Document ID: EPA-HQ-OW-2002-0039-0318
Agency: epa
Document Type: Supporting & Related Material
Title: 
Posted Date: 2003-08-05T04:00Z

Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
1
4.
Technology
Costs
4.1
Introduction
This
chapter
presents
the
estimated
capital
and
O&
M
costs
for
the
alternative
disinfection
strategies
and
DBP
precursor
removal
technologies
identified
as
potential
compliance
options
for
the
LT2ESWTR
and
the
Stage
2
DBPR.
Previous
technology
cost
estimates
were
primarily
developed
using
three
models:
the
Very
Small
Systems
Best
Available
Technology
Cost
Document
(
Malcolm
Pirnie
1993),
hereafter
referred
to
as
the
VSS
model;
the
Water
Model
(
Culp/
Wesner/
Culp
1984);
and
the
Water
and
Wastewater
(
W/
W)
Cost
Model
(
Culp/
Wesner/
Culp
2000).
The
estimates
provided
in
this
document,
however,
were
developed
largely
using
information
from
manufacturers
and
other
sources
that
are
believed
to
be
more
accurate
and
more
reflective
of
current
practices
than
the
models.
For
example,
the
use
of
manufacturer
information
is
believed
to
be
more
appropriate
for
technologies
where
costs
of
process
components
have
decreased
since
the
models
were
developed
(
e.
g.,
microfiltration/
ultrafiltration,
nanofiltration,
chloramines,
and
chlorine
dioxide).
Manufacturer
information
was
also
necessary
for
processes
that
are
not
included
in
the
models
(
i.
e.,
UV
disinfection
and
bag
and
cartridge
filters).

Costs
were
developed
for
a
range
of
design
criteria
corresponding
to
different
implementation
scenarios
and
treatment
goals
and
for
design
flows
generally
ranging
from
0.007
to
520
mgd.
Exhibit
4.1
shows
technologies
for
which
costs
were
developed
and
summarizes
the
methodology
used
to
develop
costs
(
i.
e.
cost
model,
cost
build­
up,
lump
sum
estimate,
or
a
combination).
Sections
4.2
and
4.3
describe
these
methodologies
and
explain
the
assumptions
used
for
all
cost
estimates.
Subsequent
sections
(
as
indicated
in
Exhibit
4.1)
describe
the
detailed
assumptions
used
for
each
technology
and
present
cost
estimates
in
tabular
format.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
2
Exhibit
4.1:
Technologies
Costed
and
Methodology
Used
Technology
(
Section
in
which
technology
is
costed)
Costing
Methodology
Used
Alternative
Disinfection
Strategies
Chloramination
(
section
4.4.1)
W/
W
model
for
P&
V1,
I&
C2,
cost
build­
up
for
all
other
process
and
O&
M
costs
Chlorine
dioxide
(
section
4.4.2)
W/
W
model
for
all
costs
except
CLO2
generation
equipment
leasing
costs
UV
disinfection
(
section
4.4.3)
Cost
build­
up
approach
Ozone
(
section
4.4.4)
Cost
build­
up
approach
Microfiltration
and
ultrafiltration
(
section
4.4.5)
Water
and
W/
W
cost
model
for
some
O&
M
parameters,
cost
build­
up
for
all
other
costs
Bag
and
cartridge
filtration
(
section
4.4.6)
Cost
build­
up
approach
Bank
filtration
(
section
4.4.7)
Lump
sum
estimate
using
best
professional
judgement
Second
stage
filtration
(
section
4.4.8)
Lump
sum
estimate
using
best
professional
judgement
Pre­
sedimentation
(
section
4.4.9)
Lump
sum
estimate
using
best
professional
judgement
Watershed
control
(
section
4.4.10)
Lump
sum
estimate
using
best
professional
judgement
Combined
filter
performance
(
section
4.4.11)
Cost
build­
up
approach
DBP
Precursor
Removal
Technologies
GAC
adsorption
(
section
4.5.1)
Water
model
costs
for
systems
>
0.1
mgd,
VSS
model
for
systems
<
0.1
mgd,
TOC
analyzers
by
vendor
quotes.

Nanofiltration
(
section
4.5.2)
Cost
build­
up
approach
1
P&
V
=
Pipes
and
valves.
2
I&
C
=
Instrumentation
and
controls.

4.2
Approach
for
Cost
Estimates
Following
the
reauthorization
of
the
Safe
Drinking
Water
Act
in
1996,
EPA
critically
evaluated
its
tools
for
estimating
the
costs
and
benefits
of
drinking
water
regulations.
As
part
of
this
evaluation,
EPA
solicited
input
from
national
drinking
water
experts
at
the
Denver
Technology
Workshop,
which
was
sponsored
by
EPA
and
held
November
6
and
7,
1997,
to
improve
the
quality
of
its
compliance
cost
estimating
process
for
various
drinking
water
treatment
technologies.
The
Technology
Design
Panel
(
TDP),
formed
at
the
workshop
for
this
purpose,
recommended
several
modifications
to
existing
cost
models
to
improve
the
accuracy
of
EPA's
compliance
cost
estimates
(
USEPA
1998a).
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
3
In
2001,
the
NDWAC
convened
the
Arsenic
Cost
Working
Group
to
review
the
cost
methodologies,
assumptions,
and
information
underlying
the
system­
size
cost
estimates
presented
in
the
December
2000
technologies
and
costs
document,
as
well
as
the
aggregated
national
cost
estimate,
for
the
Arsenic
Rule.
As
part
of
the
review,
NDWAC
made
several
recommendations
that
have
since
been
incorporated
into
the
cost
approach
applied
for
the
Arsenic
Rule.
This
document
incorporates
both
the
TDP
and
NDWAC
recommendations,
as
appropriate.

4.2.1
Cost
Components
and
Capital
Cost
Multipliers
Capital
Costs
For
the
purposes
of
this
document,
capital
costs
are
divided
into
three
main
components:

°
Process
costs,
which
include
manufactured
equipment,
concrete,
steel,
E&
I
(
sometimes
referred
to
as
instrumentation
and
controls
[
I&
C]),
and
pipes
and
valves
(
P&
V).

°
Construction
and
engineering
costs.
Construction
costs
include
installation,
sitework
and
excavation,
subsurface
considerations,
standby
power,
contingencies,
and
interest
during
construction.
Engineering
costs
include
general
contractor
overhead
and
profit,
engineering
fees,
and
legal,
fiscal,
and
administrative
fees.

°
Indirect
costs,
which
include
housing,
permitting,
land,
operator
training,
piloting,
and
public
education
(
these
are
not
needed
for
all
technology
types).

The
sum
of
process
and
construction
and
engineering
costs
is
often
referred
to
as
"
direct"
capital
costs.
The
TDP
recommended
that
total
capital
cost
estimates
be
based
on
process
costs,
which
are
then
multiplied
by
a
specific
cost
factor
to
estimate
direct
capital
costs.
The
NDWAC
recommendations
were
similar;
however,
the
factors
recommended
by
the
two
groups
varied
to
some
degree.
This
document
primarily
utilizes
cost
factors
recommended
by
NDWAC,
slightly
modified
as
follows:

°
A
cost
factor
of
2.5
is
used
for
systems
less
than
1.0
mgd
°
A
cost
factor
of
2.0
is
applied
for
systems
greater
than
1.0
mgd
The
cost
factor
for
systems
greater
than
1.0
mgd
is
different
from
the
1.8
value
recommended
by
NDWAC
in
order
to
account
for
installation.
For
some
small
package
technologies
(
e.
g.,
GAC
or
MF/
UF),
a
revised
multiplier
of
1.67
or
1.2
is
used
instead
of
2.5.
The
basis
for
the
revised
multipliers
is
that
the
2.5
multiplier
is
applicable
to
relatively
inexpensive
technologies
that
require
proportionally
greater
engineering
and
design
effort
than
small
package
systems.
In
addition,
many
of
the
package
technologies
considered
in
this
document
are
significantly
more
expensive
than
conventional
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
4
technologies,
yet
installation
is
typically
much
less
complicated
than
traditional
non­
packaged
technologies.
These
alternate
cost
multipliers
were
developed
using
vendor
quotes
and
experience
with
similar
systems.
Exhibit
4.2
summarizes
the
components
of
each
of
the
capital
cost
multipliers
used
in
this
document.

Exhibit
4.2:
Summary
of
Capital
Cost
Multiplier
Components
Component
1.20
1.67
1.76
2.0
2.5
Site
work
­­
10%
15%
15%
25%

Contractor
OH&
P*
­­
10%
12%
10%
20%

Contingencies
­­
15%
10%
20%
30%

Engineering
and
design
­­
10%
20%
15%
25%

Mobilization
and
bonding
­­
5%
­­
3%
5%

Legal
and
administrative
­­
 
11%
10%
15%

Interest
during
construction
­­
7%
­­
7%
10%

Installation
20%
10%
­­
20%
20%

Permitting
­­
­­
3%
­­
­­

Standby
Power
­­
­­
5%
­­
­­

*
OH&
P=
overhead
and
profit
Indirect
capital
costs
are
added
to
direct
capital
costs
to
produce
total
capital
costs.
The
following
equation
indicates
how
total
capital
costs
are
calculated.

Total
Capital
Costs
=
Direct
Costs
+
Indirect
Costs
Where:
Direct
Costs
=
Process
Costs
*
Capital
Cost
Multiplier
Indirect
Costs
=
Additional
items
developed
by
the
cost
build­
up
approach
that
are
not
multiplied
by
the
capital
cost
multiplier,
such
as
land,
housing,
operator
training,
and
piloting.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
5
O&
M
Costs
O&
M
costs
represent
the
annual
costs
required
to
operate
the
technology.
O&
M
costs
include
items
such
as
labor,
chemicals,
power,
and
replacement
parts.
Each
item
is
added
(
without
multipliers)
to
produce
total
O&
M
costs.

4.2.2
Cost
Indices
and
Unit
Cost
Inputs
To
compare
the
estimated
national
costs
to
monetized
benefits
(
for
EPA
proposed
drinking
water
rules),
it
is
necessary
to
use
a
consistent
time
value
of
money
for
all
cost
estimates.
In
this
document
all
costs
are
presented
in
year
2000
dollars.
In
order
to
adjust
all
costs
to
the
same
year,
cost
indices
are
used.
Several
different
indices
are
used
in
the
cost
models
and
are
listed
in
Exhibit
4.3.
For
all
costs
not
developed
using
the
models,
the
Engineering
News
Record
(
ENR)
Building
Cost
Index
(
BCI)
is
used
(
BCI
for
year
2000
is
also
shown
in
Exhibit
4.3).
The
BCI
is
developed
to
reflect
the
cost
of
building
across
the
country.
It
represents
costs
of
labor,
steel,
concrete,
and
wood
averaged
across
20
different
cities.
To
use
it
to
adjust
costs,
the
cost
is
multiplied
by
the
ratio
of
the
index
in
the
year
desired
to
the
year
in
which
the
cost
was
developed.
For
example
if
a
cost
were
developed
using
year
2001
vendor
quotes
it
would
be
multiplied
by
the
BCI
index
for
year
2000
(
3,539)
and
divided
by
the
index
for
year
2001
(
3,574).
Thus
if
the
cost
were
$
2,500
dollars
in
year
2001
it
would
be
$
2,500*(
3,539/
3,574)
=
$
2,475.52
in
year
2000
dollars.

Exhibit
4.3:
Costs
Indices
Used
in
the
Water
and
W/
W
Cost
Models
Description
Index
Reference
Numerical
Value1
Concrete
Ingredients
and
Related
Products
BLS
132
474.6
Electrical
Machinery
and
Products
BLS
117
351.1
General
Purpose
Machinery
and
Equipment
BLS
114
455.8
Metals
and
Metal
Products
(
Steel)
BLS
1017
375.2
Miscellaneous
General
Purpose
Equipment
(
Pipes
&
Valves)
BLS
1149
504.1
Chemicals
and
Allied
Products
BLS
06
457.8
Producer
Price
Index
(
PPI)
Finished
Goods
Index
BLS
3000
392.0
ENR
Building
Cost
Index2
3539
1
BLS
numerical
values
were
re­
based
to
1967
base
year.
2
ENR
BCI
value
for
other
years
are
available
at
www.
enr.
com
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
6
Energy
and
labor
are
required
to
operate
most
technologies.
Exhibit
4.4
displays
costs
used
for
energy
and
labor
in
this
document.
Chemicals
are
also
required
for
some
technologies.
Exhibit
4.5
displays
costs
for
chemicals
required
to
operate
the
technologies
costed
in
this
document.

Exhibit
4.4:
Unit
and
General
Cost
Assumptions
Unit
Cost*

Electricity1,2
$
0.076/
kWh
Diesel
Fuel1
$
1.48/
gallon
Natural
Gas1
$
0.009/
scf
Technical
Labor3
$
24.96/
hr
Managerial
Labor4
$
44.91/
hr
Building
Energy
Use
102.6
kWh/
ft2/
yr
1
Energy
Information
Administration
2
Includes
public
street
and
highway
lighting,
other
sales
to
public
authorities,
sales
to
railroads
and
railways,
sales
for
irrigation,
and
interdepartmental
sales.
3
BLS
2000
rate
for
Standard
Occupation
Code
(
SOC)
51­
8031
4
BLS
2000
rate
for
SOC
17­
2051
*
Where
kWh
=
kilowatt
hour;
scf
=
standard
cubic
feet;
hr
=
hour;
ft
=
feet;
and
yr
=
year.

Exhibit
4.5:
Chemical
Costs
Chemical
Cost
Units
Alum,
Dry
Stock
$
300
per
ton
Alum,
Liquid
Stock
$
230
per
ton
Carbon
Dioxide,
Liquid
$
340
per
ton
Chlorine,
1
ton
cylinder
$
280
per
ton
Chlorine,
150­
pound
cylinder
$
600
per
ton
Chlorine,
bulk
$
280
per
ton
Ferric
Chloride
$
400
per
ton
Hexametaphosphate
$
1300
per
ton
Lime,
Hydrated
$
110
per
ton
Lime,
Quick
Lime
$
100
per
ton
Phosphoric
Acid
$
650
per
ton
Polymer
$
1.00
per
lb
Potassium
Permanganate
$
2900
per
ton
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
Chemical
Cost
Units
June
2003
4­
7
Sodium
Hydroxide,
50%
$
350
per
ton
Sodium
Hypochlorite,
12%
$
1100
per
ton
Sodium
Chlorite
$
325
per
ton
Sodium
Chloride
$
100
per
ton
Sulfuric
Acid
$
100
per
ton
Surfactant,
5%
$
0.15
per
gal
Source:
Vendor
quotes
4.2.3
Cost
Build­
up
Approach
To
estimate
capital
costs
for
those
technologies
where
cost
model
estimates
were
found
to
be
inaccurate
based
on
professional
engineering
judgement
or
when
modeled
costs
were
not
available,
a
cost
build­
up
approach
was
used.
Process
components
were
identified
and
sized
using
engineering
design
principles
and
were
costed
using
estimates
from
manufacturers,
vendors,
and
field
engineers.
Several
vendor
quotes
were
used
when
possible,
and
regressions
were
developed
to
identify
the
best
fit
curves
from
these
quotes
in
many
cases
when
they
reflect
different
design
flows.
In
some
cases
(
e.
g.,
NF)
manufacturer's
estimates
were
checked
against
real­
world
installations
to
verify
cost
reasonableness.
Vendor
quotes
were
discounted
from
the
year
in
which
they
were
obtained
back
to
year
2000
dollars,
using
the
methodology
described
in
section
4.2.2.
For
other
process
cost
items
(
e.
g.,
E&
I,
P&
V)
engineering
principles
were
used
in
conjunction
with
engineering
cost
estimating
guides
such
as
RS
Means.
Such
guides
contain
nationwide
averages
for
costs
of
common
items
such
as
housing,
pumps,
and
tanks.
For
some
items,
vendor
quotes
or
cost
estimating
guides
were
not
useful
in
determining
costs.
In
these
cases
professional
engineering
judgement
was
used.
Costs
for
which
best
professional
judgement
was
used
are
generally
a
small
portion
of
the
total
overall
cost
of
a
technology.

4.2.4
Lump
Sum
Estimates
For
some
relatively
new
or
untraditional
technologies
a
large
data
set
of
cost
data
is
not
available.
Using
a
cost
build­
up
approach
for
these
technologies
was
not
possible.
For
these
technologies
a
single
lump
sum
figure
representing
all
process
costs
was
estimated.

4.2.5
Cost
Modeling
Approach
When
one
or
more
of
the
cost
models
was
used
to
estimate
costs,
process
costs
were
determined
based
upon
the
breakdown
of
capital
costs
provided
in
the
original
model
documentation.
Process
costs
were
then
multiplied
by
the
appropriate
cost
multipliers
(
as
discussed
in
section
4.2.1)
to
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
8
estimate
total
direct
costs.
Capital
cost
breakdowns
for
all
technologies
costed
using
the
VSS
model
are
presented
in
Appendix
A.
The
reports
Estimation
of
Small
System
Water
Treatment
Costs
(
Culp/
Wesner/
Culp
1984)
and
Estimating
Treatment
Costs,
Volume
2:
Cost
Curves
Applicable
to
1
to
200
mgd
Treatment
Plants
(
Culp/
Wesner/
Culp
1979)
were
used
to
develop
capital
cost
breakdown
summaries
for
the
Water
and
W/
W
Cost
models.
These
summaries
are
presented
in
Appendix
B
and
C,
respectively.

Sections
4.2.4.1,
4.2.4.2,
and
4.2.4.3
briefly
demonstrate
how
the
capital
cost
breakdowns
are
applied
and
how
total
direct
capital
cost
estimates
are
generated.

4.2.5.1
VSS
Model
The
VSS
model
presents
capital
and
O&
M
costs
as
functions
of
design
and
average
flow,
respectively.
Accordingly,
the
capital
cost
equation
for
a
package
GAC
plant
is:

CAP
=
1.7[
EBCT]
0.54
[
DES]
0.54
Where:
CAP
=
Total
Capital
Cost,
$
1,000s
EBCT
=
Empty
Bed
Contact
Time,
minutes
DES
=
Design
Treated
Flow,
kgpd
(
thousand
gallons
per
day)

Thus,
for
a
0.037
mgd
(
37
kgpd)
plant
with
an
EBCT
of
10
minutes,
the
capital
cost
is:

CAP
=
1.7[
10]
0.54
[
37]
0.54
CAP
=
41.4
or
$
41,400
The
VSS
model
equations
produce
estimates
in
year
1993
dollars.
To
escalate
to
year
2000
dollars,
the
equation­
generated
capital
cost
is
multiplied
by
the
ratio
of
the
ENR
BCI
for
year
2000
to
the
1993
index
value.

$
41,400
×
(
3539/
3009)
=
$
48,700
The
escalated
capital
cost
for
a
0.024
mgd
package
microfiltration
plant
is
$
48,700.

Using
the
capital
cost
breakdown
in
Appendix
A,
the
total
process
cost
is:

$
48,700
×
0.5478
=
$
26,700
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
9
The
total
direct
capital
cost
can
then
be
calculated
using
the
capital
cost
multiplier
presented
in
Exhibit
4.2
(
1.67
in
this
case).

$
26,700
×
1.67
=
$
44,600
4.2.5.2
Water
Model
The
Water
model
output
for
a
0.27
mgd
(
270,000
gpd)
GAC
plant
with
an
EBCT
of
10
minutes
is
$
256,000
(
escalated
to
year
2000
dollars).
Using
the
capital
cost
breakdown
shown
in
Appendix
B,
the
process
costs
associated
with
process
equipment,
pipes
and
valves,
and
electrical
are:

$
256,000
×
(
0.3331
+
0.052)
=
$
98,600
(
equipment)
$
256,000
×
(
0.0324)
=
$
8,300
(
pipes
and
valves)
$
256,000
×
(
0.1034)
=
$
26,500
(
electrical)
The
total
process
cost
is
$
133,400.

This
approach
must
be
applied
to
each
unit
process
(
e.
g.,
interstage
pumping)
separately,
then
totaled
for
the
entire
treatment
process
to
estimate
the
total
process
cost.
Pipes
and
valves
and
electrical
equipment
from
various
processes
are
totaled
and
included
as
a
single
line
item
in
estimates
presented
in
this
document.

The
total
direct
capital
cost
can
then
be
calculated
by
multiplying
the
process
cost
by
the
appropriate
capital
cost
factor
(
1.67
in
this
case).

$
133,400
×
1.67
=
$
222,800
4.2.5.3
W/
W
Cost
Model
The
W/
W
Cost
model
output
for
a
10
mgd
gravity
carbon
contactor
(
EBCT
=
10
minutes)
is
$
2,198,000
(
year
2000
dollars).
Using
the
capital
cost
breakdown
shown
in
Appendix
C,
the
process
costs
associated
with
process
equipment,
pipes
and
valves,
and
electrical
are:

$
2,198,000
×
(
0.1463
+
0.0595
+
0.0455)=
$
552,400
(
equipment)
$
2,198,000
×
(
0.2353)
=
$
517,200
(
pipes
and
valves)
$
2,198,000
×
(
0.0612)
=
$
134,500
(
electrical)
The
total
process
cost
is
$
1,204,100.

This
approach
must
be
applied
to
each
unit
process
(
e.
g.,
interstage
pumping)
separately,
then
totaled
for
the
entire
treatment
process
to
estimate
the
total
process
cost.
Pipes
and
valves
and
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
10
electrical
equipment
from
various
processes
are
totaled
and
included
as
a
single
line
item
in
estimates
presented
in
this
document.

The
total
direct
capital
cost
is
then
calculated
by
multiplying
the
process
cost
by
the
capital
cost
factor
(
2.0
in
this
case).

$
1,204,100
×
2.0
=
$
2,408,200.

4.2.6
Indirect
Capital
Costs
At
the
recommendation
of
the
TDP
and
NDWAC
cost
working
groups,
total
capital
cost
estimates
include
not
only
direct
costs
(
process,
construction,
and
engineering),
but
also
the
costs
associated
with
permitting,
piloting,
land,
housing,
operator
training,
and
public
education,
when
applicable.

Permitting
Permitting
costs
can
be
highly
variable.
Some
permits
can
require
extensive
studies,
(
e.
g.,
Environmental
Assessments
(
EAs)
or
Environmental
Impact
Statements
(
EIs)).
Others
may
require
extensive
legal
assistance.
Costs
also
are
affected
by
whether
a
utility
has
the
in­
house
expertise
to
develop
and
submit
the
necessary
permits
or
if
additional
consulting
is
required.
Permitting
cost
estimates
in
this
chapter
are
assumed
to
be
three
percent
of
the
total
process
cost.
The
minimum
cost
assigned
for
permitting
is
$
2,500,
and
costs
do
not
exceed
$
500,000
for
any
system
for
which
permitting
costs
are
included.
Permitting
costs
are
assumed
to
be
included
as
a
part
of
the
engineering
fees
(
included
in
the
capital
cost
factor)
for
those
processes
requiring
minor
process
modifications
(
e.
g.,
chloramination).

Piloting
NDWAC
recommended
that
the
costs
of
pilot
tests
be
included
for
all
technologies.
For
the
purposes
of
this
document,
it
is
assumed
that
piloting
would
not
be
necessary
for
technologies
requiring
relatively
minor
process
modifications
(
e.
g.,
chloramination).
For
these
technologies,
in­
house
DBP
formation
potential
tests
would
be
sufficient.
Piloting
costs
are
also
not
included
for
technologies
where
manufacturer
studies
(
e.
g.,
the
National
Science
Foundation
(
NSF)
Environmental
Technology
Verification
reports)
may
satisfy
regulatory
agency
technology
verification
requirements
(
e.
g.,
bag
and
cartridge
filters).
All
other
technologies
include
the
costs
associated
with
bench­
or
pilot­
scale
tests.
For
systems
less
than
1
mgd,
bench­
scale
tests
are
assumed.
Pilot­
scale
tests
are
assumed
for
all
systems
larger
than
1
mgd.
Costs
are
based
on
best
professional
judgement
and
experience
with
similar
systems.
Exhibit
4.6
summarizes
the
piloting
cost
assumptions
used
in
this
document.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
11
Exhibit
4.6:
Summary
of
Piloting
Cost
Assumptions
Technology
Design
Flow
(
mgd)

<
0.1
0.1
to
1
>
1
Chloramination
$
0
$
0
$
0
Chlorine
Dioxide
$
5,000
$
10,000
$
50,000
Ozone
$
5,000
$
10,000
$
65,000
Ultraviolet
Light
$
1,000
$
1,000
10%
of
capital
$
250,000
maximum
Microfiltration
and
Ultrafiltration
$
1,000
$
10,000
$
60,000
Granular
Activated
Carbon
$
5,000
$
10,000
$
50,000
Nanofiltration
$
1,000
$
10,000
$
60,000
Land
The
majority
of
the
technologies
discussed
in
this
document
will
likely
fit
in
existing
plant
footprints,
and
additional
land
will
not
be
required.
However,
several
of
the
processes
(
i.
e.,
ozone,
MF/
UF,
GAC,
and
NF)
will
not
likely
fit
in
existing
footprints
and
may
require
utilities
to
purchase
additional
land.

Exhibit
4.7
summarizes
the
land
cost
assumptions
used
in
this
document.
The
NDWAC
cost
working
group
recommended
that
land
costs
be
included
at
two
to
five
percent
of
total
capital
costs.
This
recommendation
is
based
on
new
treatment
plant
construction
and
is
determined
to
be
excessive
for
the
purposes
of
this
document.
As
a
result,
land
costs
are
included
at
percentages
ranging
from
0.5
to
2
percent,
depending
on
the
technology.
The
percentage
varies
from
technology
to
technology
because
of
the
relative
capital
cost
of
each
technology.
For
example,
the
total
capital
cost
for
a
210
mgd
GAC
plant
is
approximately
$
37
million,
whereas
the
capital
cost
for
a
210
mgd
MF/
UF
plant
is
$
210
million.
Using
identical
percentages,
the
land
costs
for
the
MF/
UF
plant
would
be
significantly
higher
than
those
for
a
GAC
plant;
however,
the
footprint
associated
with
a
GAC
facility
is
larger
than
that
of
a
MF/
UF
system.
Land
cost
percentages
were
adjusted
to
account
for
this
discrepancy.
Percentages
were
also
adjusted
based
on
the
estimated
footprint
of
the
technology.
That
is,
if
the
land
cost
per
acre
were
considered
unreasonable,
the
percentage
was
adjusted
accordingly.
For
example,
assuming
two
percent
of
the
capital
cost,
the
land
cost
per
acre
for
a
520
mgd
MF/
UF
system
is
nearly
$
500,000,
which
is
unreasonable
based
on
best
professional
judgment,
and
the
land
cost
percentage
is,
therefore,
adjusted.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
12
Exhibit
4.7:
Summary
of
Land
Cost
Assumptions
(
as
a
percentage
of
Capital
Cost)

Technology
System
Size
(
mgd)

<
1
1
­
10
>
10
Ozone
2%
2%
2%

Microfiltration
and
Ultrafiltration
1%
1%
0.5%

Granular
Activated
Carbon
2%
2%
2%

Nanofiltration
2%
1%
0.5%

Housing
In
many
instances,
additional
building
space
will
be
constructed
at
the
treatment
plant
to
house
a
new
technology.
For
the
purposes
of
this
document,
all
housing
costs
were
calculated
by
multiplying
the
estimated
technology
footprint
size
(
ft2)
by
a
unit
housing
cost
($/
ft2).
The
footprint
size
for
each
technology
was
derived
from
the
cost
models
or
was
based
on
best
professional
judgement
and
experience
with
similar
systems.
The
unit
housing
cost
is
taken
from
the
year
2000
RS
Means
building
construction
data,
for
the
construction
of
a
"
factory"
type
building.
The
median
value
of
$
48.95/
ft2
is
assumed
for
all
technologies,
which
includes
site
work,
plumbing,
HVAC,
and
electrical.

Operator
Training
A
system
that
adds
a
significantly
different
technology
will
have
to
train
its
operators
in
the
use
of
the
new
technology.
Costs
for
this
largely
represent
the
operator's
time,
as
most
manufacturers
will
provide
free
training
with
their
products.
The
amount
of
time
will
vary
depending
on
the
complexity
of
the
technology
installed.
Some
technologies
(
e.
g.,
chloramines)
may
require
no
additional
training
because
they
are
very
similar
to
existing
systems.
Large
systems
also
often
have
regularly
scheduled
training
sessions
and
will
be
able
to
include
training
for
new
technologies
into
these
sessions.
For
this
reason,
no
additional
cost
is
included
for
large
systems
for
some
technologies
that
work
on
similar
principles
to
existing
technologies.
Costs
assumed
in
this
document
for
operator
training
range
from
$
0
to
$
25,000.

Public
Education
If
adding
a
technology
will
significantly
affect
the
properties
of
the
water
delivered
to
customers,
systems
will
need
to
spend
money
to
notify
their
customers
of
the
changes.
In
the
case
of
chloramines,
the
chloramine
residual
can
have
an
adverse
effect
on
dialysis
patients
and
owners
of
aquariums.
Therefore
costs
are
included
to
notify
the
public
of
the
change.
Costs
include
preparing
material
such
as
bill
inserts
and
employee
time
to
either
call
or
visit
specifically
affected
customers.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
13
4.3
Estimation
of
Annualized
Costs
The
models
and
other
cost
estimation
methods
are
used
to
develop
total
capital
costs
and
annual
O&
M
costs.
Capital
costs
can
be
annualized
and
converted
into
cents
per
thousand
gallons
(
¢
/
kgal)
treated
using
the
following
formula:

Annualized
Capital
Cost
=
Capital
Cost
($)
×
Amortization
Factor
×
100
¢
/
$
Average
Daily
Flow
(
mgd)
×
(
1000
kgal/
mgal)
×
365
days/
year
Where:
kgal
=
thousand
gallons
mgal
=
million
gallons
Factors
that
correspond
to
discount
rates
of
3,
7,
and
10
percent
over
20
years
are
shown
in
Exhibit
4.6.
Alternative
capital
recovery
factors
can
be
calculated
using
the
formula
presented
below.

Amortization
Factor
=
i(
1
+
i)
N
(
1
+
i)
N
­
1
Where:
i
=
discount
rate
N
=
number
of
years
Exhibit
4.8:
Amortization
Factors
Discount
Rate
(%)
Period
(
years)
Amortization
Factor
A
B
C
=
a(
1+
a)
b
(
1+
a)
b­
1
3
20
0.0672157
7
20
0.0943929
10
20
0.1174596
Annual
O&
M
costs
include
the
costs
for
materials,
chemicals,
power,
and
labor.
The
annual
O&
M
costs
can
be
converted
into
cents
per
thousand
gallons
treated
using
the
following
formula:

O&
M
Cost
(
¢
/
kgal)
=
Annual
O&
M
($)
*
100
(
¢
/
$)
Average
Daily
Flow
(
mgd)*
1000
kgal/
mgal*
365
days/
year
Total
annualized
costs
for
the
treatment
process
can
then
be
determined
by:
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
14
Total
annualized
cost
(
¢
/
kgal)
=
Annualized
Capital
Costs
(
¢
/
kgal)
+
O&
M
(
¢
/
kgal)

4.4
Alternative
Disinfection
Strategies
This
section
presents
capital
and
O&
M
cost
estimates
for
a
number
of
alternative
disinfection
strategies
capable
of
removing/
inactivating
Cryptosporidium
and/
or
reducing
DBP
formation.
Each
technology
section
presents
costs
in
tabular
format,
and
provides
a
detailed
discussion
of
how
costs
were
developed
for
that
technology.

4.4.1
Chloramination
As
explained
in
Chapter
3,
the
10th
and
90th
percentile
finished
water
chlorine
residuals
from
the
ICR
database
(
0.6
and
2.2
mg/
L,
respectively)
were
used
to
establish
two
ammonia
dosages
of
0.15
and
0.55
mg/
l
NH3­
N
based
on
a
4:
1
chlorine­
to­
ammonia
ratio.
The
base
plant
is
assumed
to
provide
the
necessary
chlorine.

Aqueous
ammonia
is
assumed
for
small
systems
(<
1
mgd),
and
anhydrous
ammonia
is
assumed
for
large
systems
(>
1
mgd).
Capital
and
O
&
M
costs
are
based
primarily
on
discussion
with
vendors
and
typical
industry
equipment
and
chemical
unit
costs.
Some
capital
process
costs
(
P&
V;
E&
I,
and
controls)
are
generated
from
the
W/
W
model.

4.4.1.1
Summary
of
Chloramine
Capital
Cost
Assumptions
Process
Costs
Capital
cost
estimates
for
conversion
to
chloramines
are
presented
in
Exhibits
4.9
and
4.10
for
ammonia
doses
of
0.15
and
0.55
mg/
L,
respectively.
Estimates
were
based
on
June
2001
dollars
and
were
adjusted
to
2000
dollars
using
the
ENR
BCI.
Assumptions
for
ammonia
systems
are
as
follows:

°
Chemical
metering
pumps
for
aqueous
ammonia:
tube
pumps
for
very
small
systems
(<
0.1
mgd),
diaphragm
pumps
for
small
systems
(
0.1
­
1
mgd).
Redundant
pumps
were
assumed.

°
Vacuum
feed
systems
for
anhydrous
ammonia:
the
system
included
redundant
vacuum
regulators,
a
flow­
proportioning
dosing
system,
a
water
softening
system
and
an
ejector.
Costs
for
feed
systems
with
different
feed
capacities
are
used
(
0
to
100
lb/
day,
and
0
to
1,000
b/
day),
as
determined
by
the
system
size
and
dose.
A
vaporizer
is
also
included
for
large
systems
using
more
than
1,000
lb/
day
of
ammonia.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
15
°
Storage
tanks
for
aqueous
ammonia:
due
to
the
small
storage
volumes,
tank
costs
were
not
included.
Aqueous
ammonia
are
assumed
to
be
pumped
directly
from
the
portable
drum
container
provided
by
the
chemical
supplier.
A
minimum
30­
day
storage
capacity
was
assumed.

°
Storage
tanks
for
anhydrous
ammonia:
based
on
discussions
with
anhydrous
ammonia
suppliers,
it
is
common
for
water
treatment
plants
to
lease
the
anhydrous
ammonia
pressure
vessels
from
the
chemical
supplier.
Hence,
capital
costs
are
not
included
for
storage
tanks
(
they
are
accounted
for
as
a
tank
lease
cost
in
the
O&
M
costs).
A
minimum
30­
day
storage
capacity
was
assumed.

°
Emergency
scrubber
system:
the
cost
of
an
emergency
scrubber
system
was
included
for
large
systems
(>
1
mgd)
storing
more
than
10,000
pounds
of
anhydrous
ammonia,
as
would
be
required
by
a
Process
Safety
Management
Plan.

°
Analyzers:
On­
line
total
chlorine
analyzer
for
small
systems
and
on­
line
chloramine
analyzer
for
large
systems.
Hand­
held
analyzer
for
small
systems
for
ammonia
and
nitrate
analysis
of
distribution
system
samples.
Desktop
analyzer
for
large
systems
for
ammonia
and
nitrate
analysis
of
distribution
system
samples.

Additional
process
costs
were
based
on
percentage
of
equipment
costs.

°
P&
V
costs
were
estimated
to
represent
18
percent
of
the
sum
of
the
previous
process
costs,
based
on
capital
cost
breakdowns
used
in
the
W/
W
cost
model.

°
E&
I
and
control
costs
were
estimated
at
20
percent
of
the
sum
of
all
previous
costs
(
including
pipes
and
valves),
based
on
capital
cost
breakdowns
used
in
the
W/
W
cost
model.

Capital
Cost
Multipliers
Total
direct
costs
were
obtained
by
applying
capital
cost
multipliers
to
the
sum
of
all
process
costs.
For
large
systems,
a
factor
of
2.0
was
used.
For
small
systems,
NDWAC
recommended
a
factor
of
2.5.
This
factor
is
applicable
to
conventional
treatment
processes
that
involve
significant
engineering,
design
and
installation
efforts.
It
was
for
this
document
the
ammonia
storage
and
feed
systems
for
very
small
and
small
systems
were
assumed
to
be
relatively
less
complex,
require
minimal
design
effort,
and
comparably
easier
to
install.
As
a
result,
the
2.5
multiplier
was
considered
excessive
for
conversion
to
chloramines,
and
a
1.67
multiplier
was
used
instead.

Indirect
Capital
Costs
Indirect
capital
costs
include
the
following:
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
16
°
Public
education
costs
of
$
10,000
to
$
50,000,
based
on
system
size
and
budget
figures
obtained
from
systems
that
implemented
chloramine
conversion.
The
estimated
costs
include
the
creation
of
informative
brochures,
visits
to
customers
most
affected
by
a
conversion
to
chloramines
(
i.
e.,
pet
stores,
hospitals),
as
well
as
ad
publication
in
the
local
newspapers.

°
Housing
costs
were
included
for
large
systems
storing
more
than
10,000
pounds
of
anhydrous
ammonia,
as
would
be
required
by
a
Process
Safety
Management
Plan.
The
housing
costs
were
calculated
by
multiplying
the
assumed
footprint
for
the
anhydrous
ammonia
storage
building
by
a
unit
cost
of
$
48.95/
ft2
based
on
RS
Means
data
(
see
section
4.2
for
more
details
on
this
unit
cost).
Building
area
ranged
from
300
to
1200
square
feet.

°
Piloting
and
permitting
costs
were
not
explicitly
costed;
these
costs
were
assumed
to
be
negligible
and
were
included
in
the
engineering
cost
(
capital
cost
factor).

4.4.1.2
Summary
of
Chloramine
O&
M
Cost
Assumptions
Exhibits
4.9
and
4.10
summarize
O&
M
costs
for
ammonia
doses
of
0.15
and
0.55
mg/
L,
respectively.
The
following
assumptions
were
used
to
estimate
O&
M
costs
associated
with
ammonia
storage
and
feed
systems:

°
Chemical
costs
were
developed
based
on
vendors'
quotations.

°
Aqueous
ammonia:
$
1,069/
ton
as
NH3
in
15­
gal
drum
$
1,027/
ton
as
NH3
in
55­
gal
drum
$
646/
ton
as
NH3
in
300­
gal
drum
°
Anhydrous
ammonia:
$
840/
ton
as
NH3
for
first
large
system
category
(
1.2
mgd
design
flow)
$
400/
ton
as
NH3
for
large
system
storing
>
10,000
lb
Costs
are
interpolated
between
these
systems
based
on
flow.

°
Tank
lease
cost
was
included
only
for
large
systems
(
anhydrous
ammonia).
Based
on
chemical
suppliers'
information
and
assuming
that
plant
operators
perform
maintenance
of
the
tanks,
the
annual
tank
lease
costs
varied
from
$
500
per
1,000­
gal
tank
to
$
800
per
4,000­
gal
tank.

°
Part
replacement
costs
were
estimated
based
on
vendors'
quotations
for
parts
anticipated
to
fail
or
be
consumed
(
i.
e.,
tube
or
diaphragm
for
chemical
metering
pumps,
reagents
for
on­
line
chloramine
analyzer).
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
17
°
Electricity
costs
were
estimated
based
on
metering
pump
power
requirements
for
small
systems
and
on
vacuum
feed
system
and
vaporizer
power
requirements
for
large
systems.
Due
to
high
energy
consumption
from
heating,
vaporizers
represent
a
significant
increase
in
electricity
cost
for
systems
using
>
1,000
lb
ammonia/
day.
The
electricity
unit
cost
is
$
0.0076/
kWh
(
from
Exhibit
4.4).

°
Labor
costs
were
estimated
as
the
sum
of
maintenance
labor
cost
and
monitoring
labor
cost.
Maintenance
labor
hours
were
assumed
to
vary
from
four
hours
per
month
for
very
small
systems
to
80
hours
per
month
for
the
largest
systems.
Monitoring
labor
hours
were
assumed
to
vary
from
0.5
hour
per
month
for
very
small
systems
to
36
hours
per
month
for
the
largest
systems.
The
distribution
system
was
assumed
to
monitor
for
nitrate
and
free
ammonia,
with
an
average
sampling
and
analytical
time
of
0.25
hours
per
analyte;
the
number
of
sampling
locations
ranges
from
one
location
each
month
for
very
small
systems
to
72
sampling
locations
each
month
for
the
largest
systems.
A
labor
rate
of
$
24.96/
hr
was
used
for
operators.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
18
Design
Flow
0.007
0.022
0.037
0.091
0.18
0.27
0.36
0.68
1
Average
Flow
0.0015
0.0054
0.0095
0.025
0.054
0.084
0.11
0.23
0.35
Total
Capital
Cost
$
27,912
$
27,912
$
27,912
$
27,912
$
29,412
$
36,440
$
37,321
$
40,454
$
51,586
Subtotal
Indirect
Capital
Costs
$
500
$
500
$
500
$
500
$
2,000
$
2,000
$
2,000
$
2,000
$
10,000
Public
education
$
500
$
500
$
500
$
500
$
2,000
$
2,000
$
2,000
$
2,000
$
10,000
Housing
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Capital
Cost
Multiplier
$
27,412
$
27,412
$
27,412
$
27,412
$
27,412
$
34,440
$
35,321
$
38,454
$
41,586
Subtotal
Process
Cost
$
16,414
$
16,414
$
16,414
$
16,414
$
16,414
$
20,623
$
21,150
$
23,026
$
24,902
Chemical
Feed
System
$
7,530
$
7,530
$
7,530
$
7,530
$
7,530
$
10,502
$
10,875
$
12,199
$
13,524
Scrubber
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Analyzer
$
4,062
$
4,062
$
4,062
$
4,062
$
4,062
$
4,062
$
4,062
$
4,062
$
4,062
Pipes
and
Valves
$
2,087
$
2,087
$
2,087
$
2,087
$
2,087
$
2,622
$
2,689
$
2,927
$
3,165
E&
I
and
controls
$
2,736
$
2,736
$
2,736
$
2,736
$
2,736
$
3,437
$
3,525
$
3,838
$
4,150
Total
Annual
O&
M
Cost
$
1,565
$
1,566
$
1,567
$
1,572
$
1,580
$
2,973
$
2,981
$
2,990
$
4,310
Chemicals
$
0
$
2
$
3
$
7
$
16
$
24
$
31
$
41
$
62
Tank
lease
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Part
Replacement
$
50
$
50
$
50
$
50
$
50
$
80
$
80
$
80
$
80
Electricity
$
67
$
67
$
67
$
67
$
67
$
124
$
124
$
124
$
124
Labor
$
$
1,448
$
1,448
$
1,448
$
1,448
$
1,448
$
2,746
$
2,746
$
2,746
$
4,044
Labor
Hours
58
58
58
58
58
110
110
110
162
Labor
Hours
Labor
Hours
2
0
0
0
0
0
0
0
0
0
Annual
O&
M
Cost
Summary
Capital
Cost
Summary
Exhibit
4.9:
Chloramines
as
Secondary
Disinfectant
Cost
Summary
­
Ammonia
Dose
=
0.15
mg/
L
Source:
Section
4.4.1
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
19
Design
Flow
1.2
2
3.5
7
17
22
76
210
430
520
Average
Flow
0.41
0.77
1.4
3
7.8
11
38
120
270
350
Total
Capital
Cost
$
80,696
$
80,696
$
80,696
$
80,696
$
95,696
$
95,696
$
95,696
$
154,366
$
413,127
$
413,127
Subtotal
Indirect
Capital
Costs
$
10,000
$
10,000
$
10,000
$
10,000
$
25,000
$
25,000
$
25,000
$
50,000
$
70,265
$
70,265
Public
education
$
10,000
$
10,000
$
10,000
$
10,000
$
25,000
$
25,000
$
25,000
$
50,000
$
50,000
$
50,000
Housing
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
20,265
$
20,265
Capital
Cost
Multiplier
$
70,696
$
70,696
$
70,696
$
70,696
$
70,696
$
70,696
$
70,696
$
104,366
$
342,862
$
342,862
Subtotal
Process
Cost
$
35,348
$
35,348
$
35,348
$
35,348
$
35,348
$
35,348
$
35,348
$
52,183
$
171,431
$
171,431
Chemical
Feed
System
$
13,871
$
13,871
$
13,871
$
13,871
$
13,871
$
13,871
$
13,871
$
25,760
$
25,760
$
25,760
Scrubber
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
84,215
$
84,215
Analyzer
$
11,093
$
11,093
$
11,093
$
11,093
$
11,093
$
11,093
$
11,093
$
11,093
$
11,093
$
11,093
Pipes
and
Valves
$
4,493
$
4,493
$
4,493
$
4,493
$
4,493
$
4,493
$
4,493
$
6,633
$
21,792
$
21,792
E&
I
and
controls
$
5,891
$
5,891
$
5,891
$
5,891
$
5,891
$
5,891
$
5,891
$
8,697
$
28,572
$
28,572
Total
Annual
O&
M
Cost
$
5,780
$
6,196
$
7,004
$
8,415
$
11,015
$
12,534
$
23,008
$
45,384
$
65,310
$
77,901
Chemicals
$
94
$
177
$
321
$
686
$
1,761
$
2,468
$
7,950
$
20,583
$
29,604
$
38,376
Tank
lease
$
0
$
0
$
0
$
0
$
500
$
500
$
500
$
1,000
$
1,200
$
1,200
Part
Replacement
$
1,284
$
1,284
$
1,284
$
1,284
$
1,284
$
1,284
$
1,284
$
1,284
$
1,284
$
1,284
Electricity
$
200
$
200
$
200
$
200
$
200
$
200
$
200
$
300
$
300
$
300
Labor
$
$
4,202
$
4,535
$
5,198
$
6,246
$
7,270
$
8,082
$
13,074
$
22,217
$
32,922
$
36,741
Labor
Hours
168
182
208
250
291
324
524
890
1319
1472
Labor
Hours
Labor
Hours
2
0
0
0
0
0
0
0
0
0
0
Annual
O&
M
Capital
Cost
Exhibit
4.9
(
continued):
Chloramines
as
Secondary
Disinfectant
Cost
Summary
­
Ammonia
Dose
=
0.15
mg/
L
Source:
Section
4.4.1
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
20
Design
Flow
0.007
0.022
0.037
0.091
0.18
0.27
0.36
0.68
1
Average
Flow
0.0015
0.0054
0.0095
0.025
0.054
0.084
0.11
0.23
0.35
Useful
Life
10
10
10
10
10
10
10
10
10
Labor
Rate
1
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
Labor
Rate
2
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
Capital
Cost
Total
Capital
Cost
$
27,912
$
27,912
$
27,912
$
27,912
$
29,412
$
36,440
$
37,321
$
40,454
$
51,586
Subtotal
Indirect
Capital
Costs
$
500
$
500
$
500
$
500
$
2,000
$
2,000
$
2,000
$
2,000
$
10,000
Public
education
$
500
$
500
$
500
$
500
$
2,000
$
2,000
$
2,000
$
2,000
$
10,000
Permitting
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Piloting
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Land
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Operator
Training
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Housing
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Capital
Cost
Multiplier
$
27,412
$
27,412
$
27,412
$
27,412
$
27,412
$
34,440
$
35,321
$
38,454
$
41,586
Subtotal
Process
Cost
$
16,414
$
16,414
$
16,414
$
16,414
$
16,414
$
20,623
$
21,150
$
23,026
$
24,902
Chemical
Feed
System
$
7,530
$
7,530
$
7,530
$
7,530
$
7,530
$
10,502
$
10,875
$
12,199
$
13,524
Scrubber
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Analyzer
$
4,062
$
4,062
$
4,062
$
4,062
$
4,062
$
4,062
$
4,062
$
4,062
$
4,062
Pipes
and
Valves
$
2,087
$
2,087
$
2,087
$
2,087
$
2,087
$
2,622
$
2,689
$
2,927
$
3,165
E&
I
and
controls
$
2,736
$
2,736
$
2,736
$
2,736
$
2,736
$
3,437
$
3,525
$
3,838
$
4,150
Annual
O&
M
Total
Annual
O&
M
Cost
$
1,566
$
1,570
$
1,575
$
1,592
$
1,623
$
3,038
$
3,065
$
3,101
$
4,478
Chemicals
$
2
$
6
$
10
$
27
$
59
$
88
$
115
$
152
$
231
Tank
lease
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Part
Replacement
$
50
$
50
$
50
$
50
$
50
$
80
$
80
$
80
$
80
Performance
monitoring
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Materials
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Electricity
$
67
$
67
$
67
$
67
$
67
$
124
$
124
$
124
$
124
Labor
$
$
1,448
$
1,448
$
1,448
$
1,448
$
1,448
$
2,746
$
2,746
$
2,746
$
4,044
Waste
Disposal
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Labor
Hours
58
58
58
58
58
110
110
110
162
Labor
Hours
Labor
Hours
2
0
0
0
0
0
0
0
0
0
Exhibit
4.10:
Chloramines
as
Secondary
Disinfectant
Cost
Summary
­
Ammonia
Dose
=
0.55
mg/
L
Source:
Section
4.4.1
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
21
Design
Flow
1.2
2
3.5
7
17
22
76
210
430
520
Average
Flow
0.41
0.77
1.4
3
7.8
11
38
120
270
350
Useful
Life
20
20
20
20
20
20
20
20
20
20
Labor
Rate
1
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
Labor
Rate
2
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
Capital
Cost
Total
Capital
Cost
$
80,696
$
80,696
$
80,696
$
80,696
$
95,696
$
129,366
$
382,253
$
474,677
$
570,244
$
710,620
Subtotal
Indirect
Capital
Costs
$
10,000
$
10,000
$
10,000
$
10,000
$
25,000
$
25,000
$
39,391
$
75,699
$
98,314
$
109,621
Public
education
$
10,000
$
10,000
$
10,000
$
10,000
$
25,000
$
25,000
$
25,000
$
50,000
$
50,000
$
50,000
Permitting
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Piloting
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Land
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Operator
Training
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Housing
$
0
$
0
$
0
$
0
$
0
$
0
$
14,391
$
25,699
$
48,314
$
59,621
Capital
Cost
Multiplier
$
70,696
$
70,696
$
70,696
$
70,696
$
70,696
$
104,366
$
342,862
$
398,979
$
471,930
$
600,999
Subtotal
Process
Cost
$
35,348
$
35,348
$
35,348
$
35,348
$
35,348
$
52,183
$
171,431
$
199,489
$
235,965
$
300,499
Chemical
Feed
System
$
13,871
$
13,871
$
13,871
$
13,871
$
13,871
$
25,760
$
25,760
$
45,575
$
71,335
$
116,910
Scrubber
$
0
$
0
$
0
$
0
$
0
$
0
$
84,215
$
84,215
$
84,215
$
84,215
Analyzer
$
11,093
$
11,093
$
11,093
$
11,093
$
11,093
$
11,093
$
11,093
$
11,093
$
11,093
$
11,093
Pipes
and
Valves
$
4,493
$
4,493
$
4,493
$
4,493
$
4,493
$
6,633
$
21,792
$
25,359
$
29,996
$
38,199
E&
I
and
controls
$
5,891
$
5,891
$
5,891
$
5,891
$
5,891
$
8,697
$
28,572
$
33,248
$
39,328
$
50,083
Annual
O&
M
Total
Annual
O&
M
Cost
$
6,037
$
6,678
$
7,875
$
10,263
$
15,174
$
18,601
$
30,967
$
79,369
$
153,192
$
195,454
Chemicals
$
351
$
659
$
1,193
$
2,534
$
6,420
$
8,936
$
15,509
$
48,975
$
110,193
$
142,843
Tank
lease
$
0
$
0
$
0
$
0
$
0
$
0
$
800
$
1,600
$
3,200
$
4,000
Part
Replacement
$
1,284
$
1,284
$
1,284
$
1,284
$
1,284
$
1,284
$
1,284
$
1,284
$
1,284
$
1,284
Performance
monitoring
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Materials
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Electricity
$
200
$
200
$
200
$
200
$
200
$
300
$
300
$
5,293
$
5,593
$
10,586
Labor
$
$
4,202
$
4,535
$
5,198
$
6,246
$
7,270
$
8,082
$
13,074
$
22,217
$
32,922
$
36,741
Waste
Disposal
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Labor
Hours
168
182
208
250
291
324
524
890
1319
1472
Labor
Hours
Labor
Hours
2
0
0
0
0
0
0
0
0
0
0
Exhibit
4.10
(
continued):
Chloramines
as
Secondary
Disinfectant
Cost
Summary
­
Ammonia
Dose
=
0.55
mg/
L
Source:
Section
4.4.1
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
22
4.4.2
Chlorine
Dioxide
Chlorine
dioxide
costs
were
evaluated
at
an
applied
dose
of
1.25
mg/
L.
As
explained
in
Chapter
3,
this
is
a
conservative
maximum
dose
for
compliance
with
the
chlorite
MCL
of
1
mg/
L,
assuming
70
percent
conversion
of
chlorine
dioxide
to
chlorite
and
allowing
for
impurities
in
chlorine
dioxide
generation.
This
cost
analysis
did
not
assess
the
level
of
Cryptosporidium
inactivation
that
would
be
achieved
by
this
dose,
which
would
depend
on
water
quality
and
contact
time.
The
chlorine
dioxide
costs
presented
assume
the
existing
plant
has
sufficient
contact
time
(
i.
e.,
basin
volume)
to
provide
the
required
CT.
All
costs
are
for
automatic
generation
systems.
Because
of
the
level
of
operator
attention
and
knowledge
required
to
ensure
compliance
with
the
chlorite
MCL
and
the
safety
concerns
surrounding
chlorine
dioxide
generation,
this
technology
was
assumed
to
be
inappropriate
for
systems
serving
fewer
than
500
people.
Therefore
no
costs
were
developed
for
flows
less
than
0.091
mgd.

For
systems
treating
less
than
2
mgd,
vendor
quotations
for
rental
of
chlorine
generation
equipment
were
used
(
these
are
shown
as
an
O&
M
item).
The
remainder
of
the
capital
cost
line
items
for
small
systems
were
estimated
using
the
W/
W
Cost
model.
Capital
costs
for
the
systems
treating
at
least
2
mgd
were
also
generated
using
the
W/
W
Cost
model.
In
addition,
O&
M
costs
for
all
systems
were
estimated
using
the
W/
W
Cost
model.

Costs
for
chlorine
dioxide
addition
are
presented
in
Exhibit
4.12.
Detailed
summaries
of
the
capital
and
O&
M
costs
assumptions
are
presented
below.

4.4.2.1
Summary
of
Chlorine
Dioxide
Capital
Cost
Assumptions
Process
Costs
Capital
costs
were
estimated
based
on
cost
estimating
models
and
vendor
information.
Vendor
quotes
were
obtained
in
June
2001
and
adjusted
to
year
2000
dollars
using
the
ENR
BCI.
This
section
presents
line
item
costs
for
the
various
components
that
contribute
to
the
total
capital
costs.

Feed
Equipment
Feed
equipment
costs
for
systems
with
design
capacities
above
2
mgd
were
estimated
using
the
W/
W
Cost
model.
Assumptions
for
feed
equipment
in
the
model
include
a
sodium
chlorite
mixing
and
metering
system,
a
chlorine
dioxide
generator
(
0.2
minute
detention
time),
a
polyethylene
day
tank
and
mixer,
and
a
dual
head
metering
pump.

For
design
capacities
less
than
2
mgd,
utilities
can
lease
the
equipment
for
less
money
than
they
would
spend
constructing
their
own
systems.
As
a
result,
vendor
quotations
for
equipment
leasing
were
used
instead
of
capital
equipment
costs
for
these
plants.
These
leasing
costs
were
included
in
annual
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
23
O&
M
estimates
rather
than
capital
costs.
Note
that,
although
feed
equipment
is
leased
for
systems
treating
less
than
2
mgd,
they
still
incur
capital
costs
for
instrumentation
and
controls.

Instrumentation
&
Controls,
and
Pipe
&
Valves
The
W/
W
Cost
model
was
used
to
estimate
these
line
item
capital
costs
for
all
plant
design
capacities.
The
calculation
method
for
these
capital
cost
line
items
is
not
explicitly
stated
in
the
W/
W
Cost
model
documentation;
however,
the
costs
developed
in
the
model
were
based
on
quantity
takeoffs
from
actual
and
conceptual
designs
and
information
from
actual
plant
construction
projects
as
well
as
equipment
supplier
quotations.

Capital
Cost
Multipliers
The
feed
equipment,
I&
C,
and
P&
V
capital
cost
items
were
added
to
obtain
a
subtotal
representing
process
costs.
The
process
cost
subtotal
was
multiplied
by
the
capital
cost
factor
(
2.5
for
small
systems
<
1
mgd
or
2.0
for
large
systems
$
1
mgd)
to
produce
total
direct
capital
costs.
A
complete
discussion
of
capital
cost
factors,
including
the
components
that
make
up
the
costs,
is
presented
in
section
4.2.1.

Indirect
Capital
Costs
Permitting
Significant
process
improvements
will
likely
require
coordination
with
the
appropriate
regulatory
agency.
As
such,
permitting
costs
were
included
at
three
percent
of
the
process
cost.
Minimum
($
2,500)
and
maximum
($
500,000)
permitting
costs
were
assumed.

Pilot/
Bench
Testing
The
necessity
for
pilot­
or
bench­
scale
testing
was
assumed
to
ensure
that
chlorine
dioxide
use
would
be
compatible
with
the
current
treatment
process
at
a
given
plant.
The
level
of
testing
required
was
estimated
based
on
system
size.
For
systems
less
than
0.1
mgd,
a
lump
sum
of
$
5,000
was
assumed
for
testing.
For
systems
from
0.1
to
1
mgd,
a
lump
sum
of
$
10,000
was
assumed
for
testing.
For
systems
greater
than
1
mgd,
a
lump
sum
$
50,000
was
assumed
for
testing.

Chlorine
Dioxide
System
Housing
Housing
costs
for
a
chlorine
dioxide
system
include
the
cost
for
a
building
to
house
the
equipment
and
associated
appurtenances
(
i.
e.,
heating,
ventilation
and
air
conditioning
(
HVAC),
etc.).
The
footprint
(
area)
required
to
house
the
equipment
for
each
size
system
is
calculated
in
the
W/
W
Cost
model.
The
areas,
calculated
in
square
feet,
were
then
priced
using
the
RS
Means
median
price
of
$
48.95/
ft2
for
a
factory
building.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
24
4.4.2.2
Summary
of
Chlorine
Dioxide
O&
M
Cost
Assumptions
Chlorine
dioxide
operations
and
maintenance
costs
were
estimated
using
the
W/
W
Cost
model.
Cost
factors
for
chemicals
($/
ton),
electricity
($/
kWh),
and
labor
($/
hour),
as
shown
in
Exhibit
4.4,
were
used
to
calculate
line
item
O&
M
costs.
The
sections
below
address
specifics
of
the
line
O&
M
costs.

Feed
Equipment
(
systems
smaller
than
2.0
mgd)

As
previously
mentioned,
it
is
more
cost
effective
for
systems
with
design
capacities
less
than
2
mgd
to
lease
rather
than
purchase
chlorine
dioxide
feed
equipment.
An
equipment
lease
fee
of
$
6.50
per
day
was
included
for
systems
less
than
2
mgd.
This
estimate
was
based
on
information
provided
by
chlorine
dioxide
equipment
manufacturers
that
lease
feed
equipment.
Feed
equipment
costs
for
systems
larger
than
2
mgd
were
included
as
capital
cost
items.

Chemical
Usage
Chlorine
dioxide
costs
were
evaluated
at
an
applied
dose
of
1.25
mg/
L.
Chemical
usage
was
calculated
within
the
W/
W
Cost
model
assuming
a
1:
1
mass
ratio
of
sodium
chlorite
to
chlorine.
The
theoretical
ratio
of
sodium
chlorite
to
chlorine
is
2.68:
1.
However,
chlorine
is
normally
overdosed
to
ensure
complete
conversion
of
sodium
chlorite;
the
remaining
chlorine,
when
in
solution,
is
converted
to
hypochlorous
acid
and
lowers
the
pH,
which
improves
the
chlorine
dioxide
production
efficiency.

Materials,
Electricity,
and
Labor
The
materials
costs,
kilowatt
hours
(
kWh)
of
electricity,
and
labor
hours
were
calculated
within
the
W/
W
Cost
model.
Material
costs
include
all
supplies
necessary
for
routine
maintenance
on
the
system,
such
as
gaskets,
oil
for
pumps,
spare
fittings,
etc.
Exhibit
4.11
presents
the
values
calculated
by
the
model.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
25
Exhibit
4.11:
W/
W
Cost
Model
Electricity
Usage
and
Required
Labor
Average
Flow
(
MGD)
Materials
Costs
($/
year)
Electricity
Usage/
Year
(
kWh)
O&
M
Labor/
Year
(
hours)
O&
M
Labor/
Day
(
hours)

0.025
1,708
3,437
421
1.1
0.054
2,026
3,437
454
1.2
0.084
2,239
3,437
475
1.3
0.11
2,320
3,437
482
1.3
0.23
2,542
3,437
500
1.3
0.35
2,748
3,437
517
1.4
0.41
2,866
3,443
526
1.4
0.77
3,499
3,457
577
1.6
1.4
3,952
3,504
619
1.7
3.0
4,315
3,638
667
1.8
7.8
5,444
3,917
816
2.2
11.0
5,954
4,163
897
2.5
38.0
7,463
7,241
1,356
3.7
120.0
11,157
15,165
2,548
7.0
270.0
13,957
24,749
3,835
11
350.0
15,451
29,766
4,521
12
Source:
W/
W
model
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
26
Design
Flow
(
MGD)
0.007
0.022
0.037
0.091
0.18
0.27
0.36
0.68
1
Average
Flow
(
MGD)
0.0015
0.0054
0.0095
0.025
0.054
0.084
0.11
0.23
0.35
Capital
Cost
Summary
Total
Capital
Cost
$
31,610
$
37,514
$
38,282
$
39,139
$
41,955
$
39,109
Subtotal
Indirect
Capital
Costs
$
12,827
$
17,827
$
17,827
$
17,827
$
17,827
$
17,827
Piloting
$
5,000
$
10,000
$
10,000
$
10,000
$
10,000
$
10,000
Permitting
$
2,500
$
2,500
$
2,500
$
2,500
$
2,500
$
2,500
Land
Operator
Training
Housing
$
5,327
$
5,327
$
5,327
$
5,327
$
5,327
$
5,327
Housing
SF
109
109
109
109
109
109
Other
Indirect
Costs
Capital
Cost
Multiplier
$
18,782
$
19,686
$
20,454
$
21,311
$
24,128
$
21,282
Subtotal
Process
Cost
$
7,513
$
7,875
$
8,182
$
8,525
$
9,651
$
10,641
Pipes
and
Valves
$
1,630
$
1,821
$
1,986
$
2,171
$
2,777
$
3,310
Instrumentation
and
controls
$
5,883
$
6,054
$
6,195
$
6,354
$
6,874
$
7,331
Pumping
Chlorine
Dioxide
Generator
Storage
Tanks
Process
Monitoring
Equipment
Feed
Equipment
Other
Process
Cost
#
2
Annual
O&
M
Cost
Summary
Total
Annual
O&
M
Cost
$
14,880
$
16,053
$
16,826
$
17,105
$
17,922
$
18,685
Feed
Equipment
$
2,373
$
2,373
$
2,373
$
2,373
$
2,373
$
2,373
Chemicals
$
30
$
61
$
97
$
121
$
266
$
399
Part
Replacement
Performance
monitoring
Materials
$
1,708
$
2,026
$
2,239
$
2,320
$
2,542
$
2,748
Electricity
261
$
261
$
261
$
261
$
261
$
261
$
Electricity
Use
(
kWh)
3,437
3,437
3,437
3,437
3,437
3,437
Labor
$
$
10,508
$
11,332
$
11,856
$
12,031
$
12,480
$
12,904
Labor
Hours
421
454
475
482
500
517
Data
Not
Used
Data
Not
Used
Exhibit
4.12:
Chlorine
Dioxide
Cost
Summary
Note:
Based
on
ClO2
dose
=
1.25
mg/
L
Source:
Section
4.4.2
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
27
Design
Flow
(
MGD)
1.2
2
3.5
7
17
22
76
210
430
520
Average
Flow
(
MGD)
0.41
0.77
1.4
3
7.8
11
38
120
270
350
Capital
Cost
Summary
Total
Capital
Cost
$
79,647
$
81,086
$
185,629
$
205,304
$
259,851
$
287,126
$
582,407
$
866,583
$
1,204,376
$
1,323,707
Subtotal
Indirect
Capital
Costs
$
58,098
$
58,821
$
60,177
$
63,520
$
70,300
$
73,364
$
106,528
$
167,763
$
262,267
$
298,619
Piloting
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
Permitting
$
2,500
$
2,500
$
2,500
$
2,500
$
2,843
$
3,206
$
7,138
$
10,482
$
14,132
$
15,376
Land
Operator
Training
Housing
$
5,598
$
6,321
$
7,677
$
11,020
$
17,457
$
20,157
$
49,390
$
107,281
$
198,135
$
233,243
Housing
SF
114
129
157
225
357
412
1,009
2,192
4,048
4,765
Other
Indirect
Costs
Capital
Cost
Multiplier
$
21,549
$
22,264
$
125,452
$
141,784
$
189,551
$
213,763
$
475,879
$
698,820
$
942,109
$
1,025,087
Subtotal
Process
Cost
$
10,775
$
11,132
$
62,726
$
70,892
$
94,775
$
106,881
$
237,939
$
349,410
$
471,055
$
512,544
Pipes
and
Valves
$
3,318
$
3,339
$
3,378
$
3,476
$
4,761
$
5,581
$
14,455
21,601
$
29,059
$
31,601
$
Instrumentation
and
controls
$
7,456
$
7,793
$
8,423
$
9,979
$
14,128
$
16,164
$
38,204
56,679
$
76,615
$
83,420
$
Pumping
Chlorine
Dioxide
Generator
Storage
Tanks
Process
Monitoring
Equipment
Feed
Equipment
$
50,924
$
57,437
$
75,886
$
85,136
$
185,280
271,130
$
365,381
$
397,522
$
Other
Process
Cost
#
2
Annual
O&
M
Cost
Summary
Total
Annual
O&
M
Cost
$
19,100
$
21,419
$
21,327
$
24,665
$
35,050
$
41,359
$
85,583
$
214,036
$
422,373
$
533,451
Feed
Equipment
$
2,373
$
2,373
Chemicals
$
471
$
883
$
1,658
$
3,425
$
8,941
$
12,699
$
43,724
138,128
$
310,813
$
402,894
$
Part
Replacement
Performance
monitoring
Materials
$
2,866
$
3,499
$
3,952
$
4,315
$
5,444
$
5,954
$
7,463
11,157
$
13,957
$
15,451
$
Electricity
262
$
263
$
266
$
276
$
298
$
316
$
550
$
1,153
$
1,881
$
2,262
$
Electricity
Use
(
kWh)
3,443
3,457
3,504
3,638
3,917
4,163
7,241
15,165
24,749
29,766
Labor
$
$
13,129
$
14,402
$
15,450
$
16,648
$
20,367
$
22,389
$
33,846
$
63,598
$
95,722
$
112,844
Labor
Hours
526
577
619
667
816
897
1,356
2,548
3,835
4,521
Exhibit
4.12
(
continued):
Chlorine
Dioxide
Cost
Summary
Note:
Based
on
ClO2
dose
=
1.25
mg/
L
Source:
Section
4.4.2
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
1Two
manufacturers'
estimated
costs
for
LP
lamp
systems.
These
quotes
were
averaged
to
estimate
the
equipment
and
components
of
the
O&
M
costs.
Four
manufacturers'
quotes
were
averaged
to
estimate
the
equipment
and
O&
M
costs
for
large
systems
(>
1
mgd).
June
2003
4­
28
4.4.3
Ultraviolet
Light
UV
disinfection
is
a
potential
alternative
to
chemical
disinfection.
Costs
were
estimated
for
median
post­
filter
water
quality
based
on
data
collected
during
the
ICR.
See
Chapter
3
for
the
water
quality
conditions
assumed
for
all
UV
costs.

LP
UV
lamp­
based
systems
were
assumed
for
all
systems
treating
<
1
mgd.
For
systems
treating
>
1
mgd,
cost
estimates
reflect
either
LPHO
or
medium
pressure
lamp
systems.
Manufacturer/
vendor
supplied
information
was
used
to
determine
equipment
costs,
replacement
parts
costs,
and
estimates
of
labor
and
power
requirements1.
Best
professional
judgement
and
engineering
estimates
were
used
to
assess
other
associated
costs.
Costs
for
UV
disinfection
are
summarized
in
Exhibits
4.13
through
4.16.

4.4.3.1
Summary
of
UV
Disinfection
Capital
Cost
Assumptions
Capital
costs
were
developed
from
manufacturer/
vendor
supplied
information
and
best
professional
judgment.
Equipment
costs
were
obtained
from
vendors
in
February
2002
and
adjusted
to
year
2000
dollars
using
the
ENR
BCI.
For
large
systems
(
serving
>
1
mgd),
UV
equipment
costs
represent
only
a
portion
of
the
total
process
costs.
Additional
process
costs
were
estimated
for
instrumentation
and
controls,
interstage
pumping,
piping
and
valves,
and
housing.
For
small
systems
(
flows
<
1.0
mgd),
additional
process
costs
were
assumed
to
be
captured
in
the
capital
cost
multiplier.
Indirect
capital
costs
(
for
both
large
and
small
systems)
include
pilot
testing,
training,
and
spare
parts.

Process
Costs
Manufacturers
were
asked
to
provide
UV
equipment
cost
estimates
based
on
the
anticipated
UV
system
layout
(
based
on
the
specified
number
of
reactors
as
show
in
Exhibit
3.6,
building
size,
piping,
etc.)
and
a
given
water
quality
(
see
Exhibit
3.5).
The
costs
associated
with
UV
system
validation
were
assumed
to
be
0.5
percent
of
the
manufacturers'
quotes.
System
validation
costs
were
included
in
the
UV
equipment
cost
line
item
in
Exhibits
4.13
through
4.16.

For
large
systems,
UV
process
costs
include
estimates
for
interstage
pumping
of
filter
effluent
to
UV
facilities
prior
to
storage
because
many
plants
will
not
be
able
to
retrofit
the
UV
system
into
the
existing
hydraulic
gradeline.
Costs
for
the
pump
equipment
were
supplied
by
pump
vendors.
Instrumentation
and
controls
(
including
HVAC
and
electrical)
were
assumed
to
be
20
percent
of
the
total
equipment
value
for
larger
systems.
Pipes
and
valving
were
calculated
from
vendor
quotes.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
29
Costs
were
developed
with
and
without
a
UPS
that
could
be
used
to
prevent
UV
system
shut
downs.
To
determine
the
costs
of
the
UPS
system,
three
manufacturers
were
contacted.
Their
costs
were
based
on
the
power
supply
(
i.
e.,
3
phase
240
volt),
total
kilowatts
(
kW)
necessary,
and
the
minutes
of
backup
necessary
if
a
total
power
outage
occurred.
The
power
supply
and
the
total
kW
needed
were
determined
based
on
manufacturer
information
and
an
assumed
battery
backup
time
of
five
minutes.

Capital
Cost
Multipliers
Capital
cost
multipliers
used
for
UV
disinfection
differ
from
those
recommended
by
NDWAC.
For
flows
less
than
1
mgd,
the
capital
cost
multiplier
is
1.2,
and
for
flows
greater
than
or
equal
to
1
mgd,
the
capital
cost
multiplier
is
1.76.
Systems
less
than
1
mgd
require
a
smaller
capital
cost
multiplier
than
other
treatment
technologies
because
small
UV
systems
do
not
need
significant
area
(
i.
e.,
new
building
not
needed),
equipment
installation
is
not
complex,
and
plant
modifications
are
minor
compared
to
other
technologies.
This
revised
multiplier
of
1.76
includes
allowances
for
permitting
(
3
percent),
sitework
and
interface
piping
(
15
percent),
legal,
fiscal,
and
administrative
fees
(
11
percent),
contractor
overhead
and
profit
(
12
percent),
subsurface
considerations
(
10
percent),
standby
power
(
5
percent),
and
engineering
(
20
percent).
The
lower
cost
multiplier
was
used
because
lower
installation
costs
and
less
site
work
are
necessary
compared
to
other
treatment
technologies.

Indirect
Capital
Costs
Pilot
testing,
operator
training,
housing,
and
a
spare
parts
inventory
are
included
as
indirect
capital
costs.
Pilot
testing
was
assumed
to
be
$
1,000
for
small
systems
(
less
than
1.0
mgd)
or
10
percent
of
the
direct
capital
costs
with
a
maximum
cost
of
$
250,000.
See
section
4.3
for
a
more
detailed
discussion
of
piloting
assumptions.
Operator
training
was
assumed
to
be
$
1,000
for
small
systems
and
ranges
from
$
3,000
to
$
25,000
for
larger
systems.
Housing
costs
were
based
on
the
estimated
UV
system
footprint
size
multiplied
by
a
median
housing
unit
costs
of
$
48.95/
ft2
(
see
Section
4.3
for
details).
Footprint
sizes
ranged
from
60
square
feet
to
52,000
square
feet.
The
spare
parts
inventory
costs
were
based
on
a
ten
percent
back­
up
of
system
equipment
including
lamps,
sleeves,
and
sensors,
with
the
exception
of
ballasts
and
ultraviolet
transmittance
(
UVT)
monitors
that
were
based
on
a
five
percent
and
one
unit
back­
up
of
system
equipment,
respectively.

4.4.3.2
Summary
of
UV
Disinfection
O&
M
Cost
Assumptions
The
O&
M
costs
reflect
labor
hours,
replacement
parts,
and
lamp
operating
information
provided
by
the
manufacturer.
The
number
of
lamps,
sensors,
and
ballasts
are
different,
depending
on
the
different
manufacturer.
Costs
for
replacement
parts
for
each
manufacturer
were
based
on
the
following
replacement
intervals:
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
30
°
LP
lamps
replaced
annually.

°
MP
lamps
replaced
every
six
months.

°
Sleeves
replaced
every
eight
years.

°
Intensity
sensors
and
reference
sensors
replaced
every
five
years.

°
Ballasts
and
UVT
monitors
replaced
every
ten
years.

The
calculated
costs
for
each
for
each
manufacturer
were
averaged
to
estimate
the
average
UV
replacement
parts
costs.

For
systems
treating
less
than
2
mgd,
one
hour
of
labor
per
month
plus
an
additional
two
hours
per
lamp
replacement
was
assumed.
For
systems
treating
more
than
2
mgd,
labor
hours
were
estimated
by
manufacturers
for
the
following
tasks:
daily
operation,
lamp
replacement
(
annually
for
low
pressure
lamps
and
every
6
months
for
medium
pressure
lamps),
quarterly
sensor
calibration,
and
cleaning
once
per
month
for
UV
systems
that
do
not
use
automatic
cleaning.
Labor
costs
were
derived
from
the
labor
hours
estimate
and
assumed
labor
rate
of
$
24.96/
hr.
(
See
section
4.2
for
a
discussion
of
the
operator
labor
rate
used
in
this
document.)

Power
requirements
were
estimated
from
manufacturer­
supplied
information
regarding
the
number
of
lamps
in
a
given
system,
the
kilowatt
draw
of
each
lamp,
the
warranty
power
setting,
and
the
average
number
of
UV
reactors
needed.
The
total
kilowatt
draw
from
each
manufacturer
was
then
determined,
and
the
average
power
consumption
(
kW)
was
calculated.
The
average
power
consumption
was
used
to
calculate
the
total
power
costs
by
multiplying
the
total
power
requirements
by
the
assumed
power
rate
of
0.076$/
kWh
(
see
Exhibit
4.4).

For
the
cost
estimates
that
included
a
UPS
system,
the
power
efficiency
of
the
UPS
was
assumed
to
be
90
percent
and
was
factored
into
the
power
costs.
In
addition,
UPS
systems
need
to
replace
the
batteries
and
electronics;
the
battery
and
electronics
life
expectancy
varied
depending
on
the
manufacturer
and
were
between
4
and
15
years.
The
replacement
costs
were
determined
for
each
manufacturer,
and
then
the
three
manufacturers'
replacement
costs
were
averaged
and
added
to
the
cost
estimates.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
31
Design
Flow
0.007
0.022
0.037
0.091
0.18
0.27
0.36
0.68
1
Average
Flow
0.0015
0.0054
0.0095
0.025
0.054
0.084
0.11
0.23
0.35
Labor
Rate
1
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
Labor
Rate
2
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
Capital
Cost
Summary
Total
Capital
Cost
$
9,924
$
12,645
$
15,329
$
24,687
$
39,068
$
52,290
$
64,184
$
95,721
$
222,584
Subtotal
Indirect
Capital
Costs
$
3,686
$
3,704
$
3,722
$
3,794
$
3,934
$
4,102
$
4,296
$
5,200
$
8,831
Training
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
Treatability
Testing
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
Spare
Parts
$
1,686
$
1,704
$
1,722
$
1,794
$
1,934
$
2,102
$
2,296
$
3,200
$
4,206
Housing
$
2,624
Capital
Cost
Multiplier
$
6,238
$
8,941
$
11,607
$
20,893
$
35,133
$
48,187
$
59,887
$
90,522
$
213,753
Subtotal
Process
Cost
$
5,198
$
7,451
$
9,673
$
17,411
$
29,278
$
40,156
$
49,906
$
75,435
$
121,451
I&
C
(
incl.
HVAC)
$
20,242
Pipes
and
Valves
$
16,978
Pumping
$
4,468
UV
reactors
$
5,198
$
7,451
$
9,673
$
17,411
$
29,278
$
40,156
$
49,906
$
75,435
$
79,763
Building
Annual
O&
M
Cost
Summary
Total
O&
M
Cost
$
3,399
$
3,429
$
3,818
$
4,579
$
4,769
$
6,119
$
6,498
$
8,159
$
9,024
Replacement
Parts
$
3,000
$
3,000
$
3,377
$
4,000
$
4,000
$
5,200
$
5,400
$
6,400
$
6,800
Power/
Electricity
$
50
$
80
$
91
$
180
$
320
$
420
$
524
$
960
$
1,400
Labor
$
$
349
$
349
$
349
$
399
$
449
$
499
$
574
$
799
$
824
Labor
Hours
14
14
14
16
18
20
23
32
33
Exhibit
4.13:
UV
Disinfection
Cost
Summary
(
40
mJ/
cm2
Without
UPS)

Source:
Section
4.4.3
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
32
Design
Flow
1.2
2
3.5
7
17
22
76
210
430
520
Average
Flow
0.41
0.77
1.4
3
7.8
11
38
38
350
Labor
Rate
1
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
$
24.96
Labor
Rate
2
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
$
44.91
Capital
Cost
Summary
Total
Capital
Cost
$
233,919
$
307,127
$
408,427
$
660,687
$
1,300,376
$
1,594,181
$
4,642,358
$
12,159,564
$
25,171,112
$
30,742,815
Subtotal
Indirect
Capital
Costs
$
10,041
$
42,581
$
62,388
$
99,674
$
203,714
$
248,477
$
585,476
$
1,206,373
$
2,374,492
$
2,914,465
Training
$
1,000
$
3,000
$
3,000
$
3,000
$
10,000
$
10,000
$
10,000
$
25,000
$
25,000
$
25,000
Treatability
Testing
$
1,000
$
26,455
$
34,604
$
56,101
$
109,666
$
134,570
$
250,000
$
250,000
$
250,000
$
250,000
Spare
Parts
$
5,161
$
8,980
$
16,141
$
16,449
$
17,823
$
18,510
$
25,927
$
44,332
$
74,549
$
86,910
Housing
$
2,880
$
4,146
$
8,642
$
24,124
$
66,225
$
85,397
$
299,549
$
887,042
$
2,024,944
$
2,552,555
Capital
Cost
Multiplier
$
223,878
$
264,545
$
346,039
$
561,013
$
1,096,661
$
1,345,704
$
4,056,882
$
10,953,191
$
22,796,620
$
27,828,350
Subtotal
Process
Cost
$
127,203
$
150,310
$
196,613
$
318,757
$
623,103
$
764,604
$
2,305,046
$
6,223,404
$
12,952,625
$
15,811,563
I&
C
(
incl.
HVAC)
$
21,201
$
25,052
$
32,769
$
53,126
$
103,850
$
127,434
$
384,174
$
1,037,234
$
2,158,771
$
2,635,260
Pipes
and
Valves
$
18,631
$
24,818
$
39,412
$
83,202
$
179,695
$
220,885
$
665,755
$
1,769,691
$
3,582,123
$
4,323,573
Pumping
$
4,903
$
7,149
$
10,850
$
21,501
$
43,355
$
52,580
$
157,358
$
458,075
$
1,077,655
$
1,376,209
UV
reactors
$
82,469
$
93,291
$
113,582
$
160,928
$
296,203
$
363,706
$
1,097,760
$
2,958,404
$
6,134,076
$
7,476,521
Building
Annual
O&
M
Cost
Summary
Total
O&
M
Cost
$
9,457
$
11,499
$
13,938
$
16,140
$
22,853
$
27,468
$
66,624
$
187,881
$
418,801
$
546,773
Replacement
Parts
$
7,100
$
8,200
$
9,689
$
10,166
$
11,605
$
13,704
$
31,629
$
80,143
$
174,324
$
246,358
Power/
Electricity
$
1,509
$
2,400
$
3,300
$
4,975
$
10,000
$
12,331
$
32,000
$
100,000
$
230,000
$
283,182
Labor
$
$
849
$
899
$
948
$
998
$
1,248
$
1,433
$
2,995
$
7,738
$
14,477
$
17,234
Labor
Hours
34
36
38
40
50
57
120
310
580
690
Exhibit
4.13
(
continued):
UV
Disinfection
Cost
Summary
(
40
mJ/
cm2
Without
UPS)

Source:
Section
4.4.3
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
33
Design
Flow
0.007
0.022
0.037
0.091
0.18
0.27
0.36
0.68
1
Average
Flow
0.0015
0.0054
0.0095
0.025
0.054
0.084
0.11
0.23
0.35
Capital
Cost
Summary
Total
Capital
Cost
$
19,937
$
24,013
$
28,088
$
42,760
$
66,942
$
91,395
$
115,849
$
202,794
$
449,368
Subtotal
Indirect
Capital
Costs
$
2,523
$
2,778
$
3,033
$
3,952
$
5,466
$
6,997
$
8,528
$
13,972
$
24,765
Training
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
Treatability
Testing
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
Spare
Parts
$
523
$
778
$
1,033
$
1,952
$
3,466
$
4,997
$
6,528
$
11,972
$
13,050
Housing
$
9,716
Capital
Cost
Multiplier
$
17,415
$
21,235
$
25,055
$
38,809
$
61,476
$
84,398
$
107,321
$
188,822
$
424,603
Subtotal
Process
Cost
$
14,512
$
17,696
$
20,879
$
32,341
$
51,230
$
70,332
$
89,434
$
157,352
$
241,252
I&
C
(
incl.
HVAC)
$
40,209
Pipes
and
Valves
$
19,120
Pumping
$
1,304
UV
reactors
$
14,512
$
17,696
$
20,879
$
32,341
$
51,230
$
70,332
$
89,434
$
157,352
$
180,618
Annual
O&
M
Cost
Summary
Total
O&
M
Cost
$
3,984
$
4,118
$
4,686
$
5,975
$
7,206
$
8,850
$
9,230
$
10,775
$
11,497
Replacement
Parts
$
3,255
$
3,324
$
3,824
$
4,969
$
5,453
$
6,614
$
6,710
$
7,010
$
7,180
Power/
Electricity
$
205
$
270
$
338
$
407
$
1,080
$
1,488
$
1,659
$
2,568
$
3,081
Labor
$
$
524
$
524
$
524
$
599
$
674
$
749
$
861
$
1,198
$
1,236
Labor
Hours
21
21
21
24
27
30
35
48
50
Exhibit
4.14:
UV
Disinfection
Cost
Summary
(
200
mJ/
cm2
Without
UPS)

Source:
Section
4.4.3
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
34
Design
Flow
1.2
2
3.5
7
17
22
76
210
430
520
Average
Flow
0.41
0.77
1.4
3
7.8
11
38
120
270
350
Capital
Cost
Summary
Total
Capital
Cost
$
489,097
$
696,192
$
1,003,788
$
1,760,142
$
3,833,256
$
4,663,129
$
13,625,666
$
35,881,035
$
72,395,074
$
87,332,636
Subtotal
Indirect
Capital
Costs
$
26,544
$
92,637
$
130,072
$
227,781
$
424,525
$
456,866
$
806,154
$
1,687,907
$
3,110,935
$
3,693,082
Training
$
1,000
$
3,000
$
3,000
$
3,000
$
10,000
$
10,000
$
10,000
$
25,000
$
25,000
$
25,000
Treatability
Testing
$
1,000
$
60,355
$
87,372
$
153,236
$
250,000
$
250,000
$
250,000
$
250,000
$
250,000
$
250,000
Spare
Parts
$
13,156
$
13,584
$
14,386
$
16,257
$
21,602
$
24,274
$
53,139
$
124,764
$
242,359
$
290,465
Housing
$
11,388
$
15,698
$
25,315
$
55,288
$
142,923
$
172,591
$
493,016
$
1,288,143
$
2,593,576
$
3,127,617
Capital
Cost
Multiplier
$
462,553
$
603,555
$
873,716
$
1,532,362
$
3,408,731
$
4,206,263
$
12,819,511
$
34,193,128
$
69,284,140
$
83,639,554
Subtotal
Process
Cost
$
262,814
$
342,929
$
496,429
$
870,660
$
1,936,779
$
2,389,922
$
7,283,813
$
19,427,914
$
39,365,988
$
47,522,474
I&
C
(
incl.
HVAC)
$
43,802
$
57,155
$
82,738
$
145,110
$
322,797
$
398,320
$
1,213,969
$
3,237,986
$
6,560,998
$
7,920,412
Pipes
and
Valves
$
22,247
$
29,862
$
46,252
$
94,755
$
224,627
$
265,312
$
704,733
$
1,795,149
$
3,585,383
$
4,317,751
Pumping
$
1,605
$
2,584
$
5,048
$
13,922
$
45,392
$
57,564
$
189,022
$
515,232
$
1,050,802
$
1,269,899
UV
reactors
$
195,160
$
253,328
$
362,391
$
616,873
$
1,343,964
$
1,668,726
$
5,176,089
$
13,879,547
$
28,168,805
$
34,014,411
Annual
O&
M
Cost
Summary
Total
O&
M
Cost
$
12,480
$
15,392
$
19,142
$
29,196
$
71,152
$
99,163
$
336,820
$
1,072,973
$
2,475,577
$
3,253,233
Replacement
Parts
$
7,810
$
9,020
$
9,680
$
11,241
$
26,605
$
35,987
$
117,149
$
364,325
$
829,259
$
1,094,885
Power/
Electricity
$
3,397
$
5,025
$
7,890
$
16,027
$
41,552
$
59,282
$
208,190
$
676,200
$
1,581,422
$
2,080,177
Labor
$
$
1,273
$
1,348
$
1,572
$
1,928
$
2,995
$
3,894
$
11,482
$
32,448
$
64,896
$
78,170
Labor
Hours
51
54
63
77
120
156
460
1300
2600
3132
Exhibit
4.14
(
continued):
UV
Disinfection
Cost
Summary
(
200
mJ/
cm2
Without
UPS)

Source:
Section
4.4.3
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
35
Design
Flow
0.007
0.022
0.037
0.091
0.18
0.27
0.36
0.68
1
Average
Flow
0.0015
0.0054
0.0095
0.025
0.054
0.084
0.11
0.23
0.35
Capital
Cost
Summary
Total
Capital
Cost
$
10,353
$
13,046
$
15,779
$
25,331
$
40,095
$
53,787
$
66,233
$
100,404
$
230,775
Subtotal
Indirect
Capital
Costs
$
3,686
$
3,704
$
3,722
$
3,794
$
3,934
$
4,102
$
4,296
$
5,200
$
15,583
Training
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
Treatability
Testing
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
Spare
Parts
$
1,686
$
1,704
$
1,722
$
1,794
$
1,934
$
2,102
$
2,296
$
3,200
$
4,206
Housing
$
9,376
Capital
Cost
Multiplier
$
6,667
$
9,343
$
12,057
$
21,536
$
36,160
$
49,684
$
61,937
$
95,204
$
215,193
Subtotal
Process
Cost
$
5,556
$
7,785
$
10,047
$
17,947
$
30,134
$
41,404
$
51,614
$
79,337
$
122,269
I&
C
(
incl.
HVAC)
$
20,378
Pipes
and
Valves
$
13,408
Pumping
$
3,831
UV
reactors
$
5,260
$
7,451
$
9,673
$
17,411
$
29,278
$
40,156
$
49,906
$
75,435
$
79,763
UPS
$
296
$
334
$
375
$
536
$
856
$
1,248
$
1,708
$
3,902
$
4,888
Annual
O&
M
Cost
Summary
Total
O&
M
Cost
$
3,435
$
3,465
$
3,880
$
4,699
$
4,970
$
6,504
$
6,995
$
9,270
$
10,672
Replacement
Parts
$
3,028
$
3,036
$
3,427
$
4,101
$
4,160
$
5,525
$
5,838
$
7,410
$
8,309
Power/
Electricity
$
58
$
80
$
104
$
198
$
360
$
480
$
583
$
1,062
$
1,540
Labor
$
$
349
$
349
$
349
$
399
$
449
$
499
$
574
$
799
$
824
Labor
Hours
14
14
14
16
18
20
23
32
33
Exhibit
4.15:
UV
Disinfection
Cost
Summary
(
40
mJ/
cm2
with
UPS)

Source:
Section
4.4.3
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
36
Design
Flow
1.2
2
3.5
7
17
22
76
210
430
520
Average
Flow
0.41
0.77
1.4
3
7.8
11
38
38
350
Capital
Cost
Summary
Total
Capital
Cost
$
243,657
$
323,334
$
432,902
$
708,178
$
1,453,660
$
1,762,788
$
4,960,741
$
12,986,777
$
27,158,603
$
33,321,353
Subtotal
Indirect
Capital
Costs
$
17,543
$
53,562
$
76,735
$
121,969
$
242,558
$
287,847
$
604,115
$
1,225,481
$
2,455,709
$
3,043,065
Training
$
1,000
$
3,000
$
3,000
$
3,000
$
10,000
$
10,000
$
10,000
$
25,000
$
25,000
$
25,000
Treatability
Testing
$
1,000
$
26,977
$
35,617
$
58,621
$
121,110
$
147,494
$
250,000
$
250,000
$
250,000
$
250,000
Spare
Parts
$
5,161
$
8,980
$
16,141
$
16,449
$
17,823
$
18,510
$
25,927
$
44,332
$
74,549
$
86,910
Housing
$
10,382
$
14,605
$
21,977
$
43,898
$
93,625
$
111,843
$
318,188
$
906,150
$
2,106,161
$
2,681,155
Capital
Cost
Multiplier
$
226,114
$
269,772
$
356,167
$
586,209
$
1,211,102
$
1,474,942
$
4,356,627
$
11,761,296
$
24,702,893
$
30,278,289
Subtotal
Process
Cost
$
128,474
$
153,279
$
202,368
$
333,073
$
688,126
$
838,035
$
2,475,356
$
6,682,554
$
14,035,735
$
17,203,573
I&
C
(
incl.
HVAC)
$
21,412
$
25,547
$
33,728
$
55,512
$
114,688
$
139,673
$
412,559
$
1,113,759
$
2,339,289
$
2,867,262
Pipes
and
Valves
$
14,847
$
20,552
$
33,299
$
74,106
$
179,692
$
220,885
$
665,755
$
1,769,691
$
3,582,123
$
4,323,573
Pumping
$
4,242
$
5,920
$
9,167
$
19,151
$
43,355
$
52,580
$
157,358
$
458,075
$
1,077,655
$
1,376,209
UV
reactors
$
82,469
$
93,291
$
113,582
$
160,928
$
296,203
$
363,706
$
1,097,760
$
2,958,404
$
6,134,076
$
7,476,521
UPS
$
5,504
$
7,969
$
12,591
$
23,376
$
54,189
$
61,192
$
141,925
$
382,625
$
902,592
$
1,160,009
Annual
O&
M
Cost
Summary
Total
O&
M
Cost
$
11,364
$
15,639
$
18,617
$
21,947
$
31,972
$
38,733
$
94,050
$
243,017
$
441,418
$
507,215
Replacement
Parts
$
8,856
$
11,100
$
14,038
$
15,476
$
19,724
$
23,739
$
55,885
$
125,379
$
174,741
$
237,098
Power/
Electricity
$
1,659
$
3,640
$
3,630
$
5,473
$
11,000
$
13,561
$
35,170
$
109,900
$
252,200
$
252,884
Labor
$
$
849
$
899
$
948
$
998
$
1,248
$
1,433
$
2,995
$
7,738
$
14,477
$
17,234
Labor
Hours
34
36
38
40
50
57
120
310
580
690
Exhibit
4.15
(
continued):
UV
Disinfection
Cost
Summary
(
40
mJ/
cm2
with
UPS)

Source:
Section
4.4.3
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
37
Design
Flow
0.007
0.022
0.037
0.091
0.18
0.27
0.36
0.68
1
Average
Flow
0.0015
0.0054
0.0095
0.025
0.054
0.084
0.11
0.23
0.35
Capital
Cost
Summary
Total
Capital
Cost
$
30,909
$
35,001
$
39,222
$
54,415
$
79,456
$
104,779
$
130,101
$
220,137
$
511,015
Subtotal
Indirect
Capital
Costs
$
2,523
$
2,778
$
3,033
$
3,952
$
5,466
$
6,997
$
8,528
$
13,972
$
18,007
Training
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
Treatability
Testing
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
$
1,000
Spare
Parts
$
523
$
778
$
1,033
$
1,952
$
3,466
$
4,997
$
6,528
$
11,972
$
13,050
Housing
$
2,957
Capital
Cost
Multiplier
$
28,386
$
32,224
$
36,189
$
50,464
$
73,991
$
97,782
$
121,573
$
206,164
$
493,008
Subtotal
Process
Cost
$
23,655
$
26,853
$
30,157
$
42,053
$
61,659
$
81,485
$
101,311
$
171,804
$
280,118
I&
C
(
incl.
HVAC)
$
46,686
Pipes
and
Valves
$
33,501
Pumping
$
2,285
UV
reactors
$
14,512
$
17,696
$
20,879
$
32,341
$
51,230
$
70,332
$
89,434
$
157,352
$
180,618
UPS
$
9,143
$
9,157
$
9,278
$
9,712
$
10,429
$
11,153
$
11,877
$
14,452
$
17,027
Annual
O&
M
Cost
Summary
Total
O&
M
Cost
$
4,779
$
6,069
$
7,385
$
9,577
$
10,537
$
14,514
$
18,324
$
20,522
$
28,384
Replacement
Parts
$
3,880
$
5,095
$
5,671
$
7,027
$
7,254
$
8,115
$
8,773
$
9,741
$
12,210
Power/
Electricity
$
375
$
450
$
1,190
$
1,950
$
2,609
$
5,649
$
8,690
$
9,583
$
14,938
Labor
$
$
524
$
524
$
524
$
599
$
674
$
749
$
861
$
1,198
$
1,236
Labor
Hours
21
21
21
24
27
30
35
48
50
Exhibit
4.16:
UV
Disinfection
Cost
Summary
(
200
mJ/
cm2
with
UPS)

Source:
Section
4.4.3
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
38
Design
Flow
1.2
2
3.5
7
17
22
76
210
430
520
Average
Flow
0.41
0.77
1.4
3
7.8
11
38
120
270
350
Capital
Cost
Summary
Total
Capital
Cost
$
554,630
$
776,710
$
1,117,153
$
1,901,906
$
4,011,326
$
5,055,982
$
14,936,240
$
39,468,919
$
79,721,825
$
96,188,922
Subtotal
Indirect
Capital
Costs
$
18,696
$
90,350
$
126,398
$
211,329
$
346,482
$
456,866
$
806,154
$
1,687,907
$
3,110,935
$
3,693,082
Training
$
1,000
$
3,000
$
3,000
$
3,000
$
10,000
$
10,000
$
10,000
$
25,000
$
25,000
$
25,000
Treatability
Testing
$
1,000
$
68,636
$
99,075
$
169,058
$
250,000
$
250,000
$
250,000
$
250,000
$
250,000
$
250,000
Spare
Parts
$
13,156
$
13,584
$
14,386
$
16,257
$
21,602
$
24,274
$
53,139
$
124,764
$
242,359
$
290,465
Housing
$
3,540
$
5,130
$
9,937
$
23,015
$
64,880
$
172,591
$
493,016
$
1,288,143
$
2,593,576
$
3,127,617
Capital
Cost
Multiplier
$
535,934
$
686,360
$
990,755
$
1,690,577
$
3,664,843
$
4,599,116
$
14,130,086
$
37,781,012
$
76,610,890
$
92,495,840
Subtotal
Process
Cost
$
304,508
$
389,977
$
562,929
$
960,555
$
2,082,297
$
2,613,134
$
8,028,458
$
21,466,484
$
43,528,915
$
52,554,455
I&
C
(
incl.
HVAC)
$
50,751
$
64,996
$
93,821
$
160,093
$
347,050
$
435,522
$
1,338,076
$
3,577,747
$
7,254,819
$
8,759,076
Pipes
and
Valves
$
37,272
$
42,870
$
62,726
$
103,129
$
204,236
$
265,312
$
704,733
$
1,795,149
$
3,585,383
$
4,317,751
Pumping
$
2,688
$
3,710
$
6,846
$
15,152
$
41,271
$
57,564
$
189,022
$
515,232
$
1,050,802
$
1,269,899
UV
reactors
$
195,160
$
253,328
$
362,391
$
616,873
$
1,343,964
$
1,668,726
$
5,176,089
$
13,879,547
$
28,168,805
$
34,014,411
UPS
$
18,636
$
25,074
$
37,144
$
65,308
$
145,776
$
186,010
$
620,537
$
1,698,809
$
3,469,105
$
4,193,318
Annual
O&
M
Cost
Summary
Total
O&
M
Cost
$
38,273
$
46,757
$
95,403
$
127,882
$
400,401
$
1,233,541
$
2,792,873
$
5,222,644
$
2,846,288
$
5,268,366
Replacement
Parts
$
12,690
$
16,974
$
53,020
$
67,201
$
187,386
$
471,286
$
1,043,822
$
3,703,224
$
1,043,822
$
3,703,224
Power/
Electricity
$
24,310
$
28,435
$
40,810
$
58,740
$
210,020
$
758,540
$
1,737,570
$
1,486,972
$
1,737,570
$
1,486,972
Labor
$
$
1,273
$
1,348
$
1,572
$
1,941
$
2,995
$
3,714
$
11,482
$
32,448
$
64,896
$
78,170
Labor
Hours
51
54
63
78
120
149
460
1300
2600
3132
Exhibit
4.16
(
continued):
UV
Disinfection
Cost
Summary
(
200
mJ/
cm2
with
UPS)

Source:
Section
4.4.3
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
39
4.4.4
Ozone
Costs
are
estimated
based
on
ozone
dosages
required
to
achieve
0.5,
1,
and
2
log
Cryptosporidium
inactivation.
Required
doses
to
meet
this
inactivation
level
were
based
on
ozone
CT
values
presented
in
Chapter
2
(
Exhibit
2.13)
and
SWAT
model
runs
for
all
ICR
plants.
(
See
Chapter
3
for
a
more
detailed
description
of
SWAT
runs
used
to
develop
ozone
dose
estimates.)
The
design
dosages
used
to
meet
the
inactivation
requirements
are
3.19
mg/
L,
5.0
mg/
L
and
7.0
mg/
L.
These
values
were
factored
into
capital
costs
and
used
to
size
facilities.
Corresponding
average
values
assumed
for
day­
to­
day
operations
are
1.78
mg/
L,
2.75
mg/
L,
and
3.91
mg/
L.
These
values
were
used
to
determine
O&
M
costs.

To
control
bromate
formation
during
ozonation,
it
may
be
necessary
to
lower
the
pH
in
certain
waters.
Separate
costs
were
estimated
for
pH
adjustment
so
that
this
cost
could
be
added
to
the
costs
of
ozonation,
where
appropriate.
The
pH
adjustment
costs
include
addition
of
a
feed
system
and
chemical
costs
to
reduce
the
pH
using
sulfuric
acid
and
to
raise
the
pH
using
caustic
(
after
ozonation).
Costs
for
pH
adjustment
were
included
as
an
indirect
capital
cost
and
were
not
multiplied
by
a
capital
cost
factor.

Ozone
costs
were
based
primarily
of
vendor
quotes
from
ozone
manufacturers.
Exhibits
4.19
through
4.21
summarize
the
capital
and
O&
M
costs
associated
with
ozone.

4.4.4.1
Summary
of
Ozonation
Capital
Cost
Assumptions
Process
Costs
Process
costs
for
ozone
include
in­
plant
pumping,
ozone
generation
system,
ozone
contactor,
off­
gas
destruction
facilities,
effluent
ozone
quench,
stainless
steel
piping
(
including
valves
and
ductwork),
electrical
and
instrumentation,
and
chemical
storage.
Process
costs
were
mostly
provided
by
equipment
vendors
in
June
2001
and
were
adjusted
to
year
2000
dollars
using
the
ENR
BCI.

In­
plant
Pumping
The
in­
plant
pumping
costs
in
Exhibits
4.19
through
4.21
include
costs
for
a
concrete
wet­
well,
vertical
turbine
constant­
speed
pumps,
piping,
valving,
manifolding,
and
all
E&
I
associated
with
the
inplant
pumping
only.
No
corrosion­
resistant
materials
(
e.
g.,
stainless
steel)
are
required
for
the
pumps.
The
in­
plant
pumping
was
designed
so
that
it
can
take
place
either
near
the
ozone
system
or
at
some
other
location
somewhat
removed
from
the
generator
and/
or
contactor.
Other
details
are
provided
below.

°
A
vertical
turbine
pump
vendor
was
contacted
and
provided
the
range
of
flow
rates
and
total
dynamic
head
(
TDH)
requirement
of
15
feet.
They
provided
budgetary
costs
for
a
set
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
40
of
pumps
(
one
duty,
one
standby)
to
meet
the
requirements.
The
costs
quoted
included
bowls,
column,
shaft,
pump
discharge
head,
and
motor.

°
Wet­
well
tankage
costs
were
estimated
using
the
same
unit
cost
curve
(
cost
vs.
volume
of
wet­
well)
developed
for
the
ozone
contactors
(
without
concrete
baffles).
Details
of
this
cost
curve
development
are
provided
in
the
section
labeled
"
Ozone
Contactor
Costs"
below.

°
Pipes,
valves,
and
E&
I
were
estimated
as
a
percentage
of
the
manufactured
equipment
(
i.
e.,
pump
cost),
based
on
the
percentages
provided
in
the
W/
W
Cost
model
for
in­
plant
pumping.

Ozone
Generation
System
Ozone
generation
costs
include
costs
for
the
ozone
generators,
feed
gas
delivery
system,
ozone
dissolution
system,
ambient
air
ozone
monitors,
and
process
monitoring
equipment
necessary
to
verify
generation
rates
and
dosing.
These
costs
were
developed
through
contacting
suppliers
of
ozone
generation
equipment.
The
vendors
were
contacted
and
given
the
oxygen
generation
rates
required
(
lbs/
day);
they
responded
with
complete
system
costs
for
all
components.

All
ozone
generation
equipment
costs
include
N+
1
redundancy;
thus,
a
minimum
of
two
ozone
generators
would
be
provided.
The
type
of
feed
gas
delivery
system
is
dependant
on
the
size
of
the
system
and,
more
specifically,
the
amount
of
ozone
required
each
day.
For
systems
requiring
less
than
100
lbs/
day
of
ozone,
oxygen
is
generated
onsite
via
pressure
swing
absorption
(
PSA).
PSA
requires
feed
gas
equipment
such
as
an
air
compressor,
air
chiller,
and
air
dryer.
For
systems
requiring
more
than
100
lbs/
day
of
ozone,
oxygen
is
provided
via
liquid
oxygen
stored
in
an
onsite
tank.
(
The
liquid
oxygen
tank
is
included
in
the
ozone
generation
equipment
heading.)

The
ozone
dissolution
system
can
consist
of
venturi­
type
injector
devices
or
porous
diffusers
in
the
ozone
contacting
tank.
Vendors
providing
cost
estimates
universally
preferred
venturi­
type
injectors
and
therefore
the
costs
are
based
on
that
type
of
ozone
dissolution.
Ozone
generation
systems
are
sized
based
on
a
transfer
efficiency
of
90
percent.
As
an
example
for
a
design
dose
of
3.19
mg/
L
(
to
meet
CT
at
0.5
log
removal),
the
actual
ozone
generation
requirement
is
estimated
as:

Ozone
generation
requirement
(
lbs/
day)
=
(
3.19
mg/
L)
×
(
design
flow)
×
(
conversion
factor)
×
(
1.1)

Ozone
Contactor
Costs
The
ozone
contactor
is
a
concrete
tank
with
a
total
hydraulic
detention
time
of
12
minutes.
N+
1
redundancy
also
applies
to
the
ozone
contactor
design.
Baffles
are
included
to
segregate
the
reactor
into
five
chambers
flowing
in
an
over/
under
configuration.
The
tank
has
a
concrete
top
to
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
41
ensure
capture
of
any
ozone
that
may
off­
gas
from
the
reactor.
Specific
design
criteria
applied
are
as
follows.
.
°
Wall
thickness
=
18
inches,
bottom
slab
and
cover
thickness
=
12
inches
°
Length­
to­
width
ratio
=
2.5
°
Water
depth
inside
the
tank
ranges
from
5
to
20
feet.

°
Design
volume
=
1.2
x
required
volume
for
freeboard
and
odor
control
connections
°
Stainless
steel
baffles
for
contactors
<
10,000
gallons
(<
1
mgd
design
flow);
concrete
baffles
for
contactors
>
10,000
gallons
(
$
1
mgd)

°
Concrete
baffle
thickness
=
8
inches
Ozone
contactor
costs
include
all
costs
related
to
installing
reinforced
concrete
tankage.
These
costs
include
excavation,
formwork,
rebar,
concrete,
backfill,
tank
coatings,
and
miscellaneous
hardware
relating
directly
to
the
tank
(
e.
g.,
railings,
hatches,
pipe
supports,
and
additions).
The
cost
does
not
include
costs
for
connecting
process
lines
or
ductwork
to
the
exterior
of
the
tank
or
connecting
instrumentation
cabling
or
required
electrical
cabling
to
the
tank.
(
These
costs
are
included
in
the
piping
and
valves
and
E&
I
process
line
items.)
With
a
given
tank
volume
estimate
(
per
design
criteria
above)
unit
costs
measured
in
terms
of
$/
cubic
yard
of
concrete
were
applied.
The
unit
costs
used
for
concrete
are
as
follows.

°
$
525/
cubic
yard
for
floors
and
slabs
°
$
675/
cubic
yard
for
walls
and
baffles
°
$
825/
cubic
yard
for
decks
These
unit
costs
were
based
on
best
professional
judgment
where
each
of
the
above
unit
costs
is
1.5
times
a
base
cost
for
concrete
work
only
(
i.
e.,
to
perform
only
the
concrete
work
with
no
excavation,
backfill,
miscellaneous
fittings,
coatings,
etc.).
Values
of
$
350,
$
450,
and
$
550
per
cubic
yard
are
commonly
used
as
budgetary
values
for
installation
of
floors,
walls,
and
decks,
respectively.
The
value
of
$
525
used
here
for
slabs
results
from
(
1.5)
×
($
350).
The
1.5
multiplier
represents
approximately
25
percent
for
excavation
and
backfill
costs
and
25
percent
for
miscellaneous
hardware
related
directly
to
the
tank.
Using
these
unit
costs
and
the
tankage
design
assumptions,
cost
vs.
contactor
volume
relations
were
developed
for
both
concrete
baffled
(>
1
mgd)
and
nonconcrete
baffled
tanks.
This
relation
was
then
applied
to
the
various
flow
categories,
noting
that
contactor
volume
is
a
function
of
design
flow,
contact
time,
and
tank
geometry
design
assumptions.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
42
Off
Gas
Destruction
Ozone
contactors
must
be
covered
and
have
systems
for
the
collection
of
the
ozone
off­
gas
because
ozone
is
toxic
and
must
be
kept
within
Occupational
Safety
and
Health
Administration
(
OSHA)
allowable
limits.
A
negative
pressure
is
maintained
in
the
headspace
of
the
contacting
basin.
Blowers
are
used
to
convey
the
gas
to
catalytic
ozone
off­
gas
destruction
devices
that
destroy
the
remaining
ozone
and
release
the
treated
gas
to
the
atmosphere.
Off­
gas
facilities
include
a
thermalcatalytic
destruct
unit,
blowers,
and
ductwork
necessary
to
convey
off­
gas
to
the
destruct
unit.

Ductwork
for
conveying
the
off­
gas
from
the
contactors
to
the
unit
and
E&
I
for
the
unit
were
not
included
in
this
line
item
cost.
(
They
are
covered
by
the
stainless
steel
piping
and
E&
I
line
items.)
E&
I
around
the
unit
was
not
included
in
this
line
item.
Off­
gas
destruction
facility
costs
were
based
on
vendor
estimates.

Effluent
Ozone
Quench
Ideally,
the
ozone
dose
provides
the
treatment
necessary
in
the
contactor
and
no
ozone
residual
is
left
as
the
treated
stream
leaves
the
contactor.
However,
this
situation
is
not
always
achieved,
and
some
ozone
residual
usually
leaves
the
reactor.
To
eliminate
downstream
reactions
outside
of
the
contactor,
the
residual
ozone
must
be
quenched
(
destroyed)
prior
to
the
next
unit
process.
The
ozone
quenching
was
assumed
to
be
conducted
with
hydrogen
peroxide
fed
from
a
storage
facility
into
the
effluent
stream
by
chemical
feed
pumps.
The
quench
system
includes
peroxide
storage,
chemical
feed
pumps,
and
a
liquid
phase
ozone
analyzer.
Design
assumptions
are
outlined
below.

°
Peroxide
is
stored
and
used
as
35
percent
solution
(
by
weight).

°
Peroxide
quenches
ozone
1:
1
by
weight.

°
Ten
percent
of
design
transferred
dose
remains
as
residual
and
requires
peroxide
quench.

°
Peroxide
storage
facilities
must
allow
for
30
days
of
storage
without
new
deliveries.

Costs
were
based
on
calls
to
vendors;
some
package
delivery
systems
were
costed
as
well
as
the
individual
components
to
build
a
complete
system.
The
following
three
quenching
systems,
based
on
dosing
requirements,
were
costed.

°
Very
small
quenching
systems
are
those
systems
dosing
less
than
100
gallons
per
month.
These
systems
were
assumed
to
store
peroxide
in
55
gallon
drums
and
dose
directly
from
the
drums
with
chemical
feed
pumps.
The
pump
controls
are
skid­
or
frame­
mounted
near
the
drums
and
pumps.
No
capital
cost
for
tankage
is
incurred;
the
drums
were
assumed
to
be
changed
by
a
chemical
supplier
(
O&
M
cost
only).
Cost
does
not
include
piping
or
valving
necessary
to
convey
peroxide
to
the
injection
location
or
E&
I
beyond
the
purchase
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
43
of
the
ozone
analyzer.
The
system
cost
is
the
sum
of
the
individual
components
as
quoted
by
vendors.

°
Small
quenching
systems
are
those
required
to
dose
between
100
and
1000
gallons
of
peroxide
per
month.
These
systems
were
assumed
to
maintain
permanent
stainless
steel
storage
tanks
on
site
in
addition
to
the
chemical
feed
pumps
and
analyzer.
The
system
cost
is
the
sum
of
the
individual
components
as
quoted
by
vendors.

°
Large
quench
systems
are
associated
with
doses
in
excess
of
1000
gallons
of
peroxide
per
month.
The
costs
were
based
on
package
systems
from
a
peroxide
supply
vendor.
The
cost
includes
a
9,600
gallon
stainless
steel
storage
tank,
skid­
mounted
dosing
pumps,
some
controls
between
the
pumps
and
the
tanks,
and
all
suction
piping
between
the
tank
and
the
chemical
feed
pump.

Chemical
Storage
A
concrete
pad
was
assumed
as
a
capital
cost
for
the
LOX
tank
and
the
peroxide
tanks
at
the
larger
dose
and
quench
requirements.
The
concrete
was
assumed
to
be
12­
inch­
thick
reinforced
concrete
with
an
installed
slab
on
grade
cost
of
$
350/
cubic
yard.

Stainless
Steel
Piping
(
Including
Valves
and
Duct
Work)

A
cost
addition
of
25
percent
of
the
sum
of
the
costs
for
the
ozone
generation
system,
ozone
contactor,
off­
gas
destruction
facilities,
and
effluent
quench
system
was
included
as
a
process
cost
line
item.
This
addition
captures
the
material
cost
of
all
piping,
valves,
fittings,
ductwork,
and
dampers
to
convey
the
liquid
and
air
streams
to
or
from
one
unit
process
to
the
next.
New
piping
and
appurtenances
for
the
liquid
stream
can
be
expected
before
and
after
the
in­
plant
pumping
facilities,
ozone
generation
system,
ozone
contactors,
and
effluent
ozone
quench
system.

Budgetary
cost
estimates
for
these
components
in
water
and
wastewater
treatment
facilities
range
widely
with
values
from
10
to
35
percent
of
the
process
costs
being
commonly
referenced.
In
the
Water
model
documentation,
pipes
and
valves
range
from
7
to
20
percent
of
the
cost
of
the
manufactured
equipment,
depending
on
the
ozone
feed
rate
(
lb/
day).
A
recent
cost
estimate
for
a
full
scale
ozone
retrofit
in
Southern
California
has
piping
(
including
valves
and
appurtenances)
at
24
percent
of
total
equipment
cost
and
27
percent
of
the
ozone
equipment
cost.
Ozone
is
very
corrosive;
therefore,
all
process
piping
that
may
come
into
contact
with
ozone
must
be
made
of
a
corrosionresistant
metal
such
as
stainless
steel.
The
value
of
25
percent
was
selected
to
represent
the
premium
paid
for
the
corrosive
resistant
piping
that
will
be
required
in
much
of
the
process.

Electrical
and
Instrumentation
(
E&
I)

A
cost
addition
of
20
percent
of
the
sum
of
the
costs
for
the
ozone
generation
system,
ozone
contactors,
off­
gas
destruction
facilities,
and
effluent
quench
system
was
included
as
a
process
cost
line
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
44
item
to
capture
the
cost
of
electrical
and
instrumentation
equipment
(
e.
g.,
cabling,
motor
control
centers,
programmable
logic
controllers
(
PLCs),
additional
ozone
analyzers,
flow
meters,
communications
cable,
software,
and
standby
power)
beyond
that
provided
with
the
ozone
generation
system
or
effluent
quench
system.
This
addition
includes
instrumentation
to
ensure
the
housing
around
the
ozone
generator
is
monitored
for
ambient
ozone
levels
(
alarm
systems
are
typically
part
of
a
monitoring
program).

Like
stainless
steel
piping,
budgetary
numbers
for
E&
I
range
widely
depending
on
the
process
and
the
source.
The
Water
model
documentation
suggests
that
E&
I
costs
as
a
percentage
of
manufactured
equipment
range
from
41
to
56
percent.
When
applied
to
the
other
components
of
the
process
not
solely
to
the
generation
equipment
the
value
of
20
percent
was
determined
to
be
representative.
The
ozone
generation
system
costs
include
much
of
the
monitoring
devices
needed
in
and
around
the
ozone
generation
systems.

pH
Adjustment
To
control
bromate
formation
during
ozonation,
it
may
be
necessary
to
lower
the
pH
in
certain
waters.
Separate
costs
were
estimated
for
pH
adjustment
so
that
this
cost
could
be
added
to
the
costs
of
ozonation,
where
appropriate.
The
pH
adjustment
costs
include
addition
of
a
feed
system
and
chemical
costs
to
reduce
the
pH
using
sulfuric
acid
and
to
raise
the
pH
using
caustic
(
after
ozonation).
Capital
costs
for
pH
reduction
were
developed
based
on
calls
to
vendors
for
significant
components
that
make
up
an
acid
feed
system.
Since
the
acid
feed
may
or
may
not
be
used
depending
on
the
system,
percentages
for
pipes
and
valves,
E&
I,
and
capital
cost
multipliers
were
estimated
separately
and
included
as
a
line
item
under
"
indirect
costs"
in
Exhibits
4.19
through
4.21.

Capital
Cost
Multipliers
Process
costs
were
estimated
and
added,
resulting
in
a
total
process
cost
at
each
flow
rate.
This
value
was
then
multiplied
by
the
appropriate
capital
cost
multiplier
(
either
2.0
for
large
systems
treating
>
1
mgd
or
2.5
for
small
systems
treating
<
1
mgd),
resulting
in
a
value
that
represents
constructed
process
facilities.

Indirect
Capital
Costs
Indirect
costs
assumed
for
the
ozone
system
include
housing,
operator
training,
land,
permitting,
and
piloting.
Housing
costs
were
based
on
the
estimated
footprint
of
the
ozone
generation
equipment
(
minimum
100
ft2),
multiplied
by
an
average
housing
cost
of
$
48.95/
ft2
based
on
RS
Means
factory
building
estimates.
Operator
training
was
assumed
as
a
capital
cost
for
systems
with
flows
less
than
1
mgd.
Forty
hours
of
training
was
assumed
at
the
technical
labor
rate
of
$
24.96/
hr.

Exhibit
4.17
shows
the
piloting
assumptions
for
ozone.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
45
Exhibit
4.17:
Ozone
Piloting
Assumptions
Flow
range
Pilot
Cost
($)

<
0.1
mgd
5,000
0.1
to
<
1.0
mgd
10,000
$
1.0
mgd
65,000
Source:
Exhibit
4.6
The
pilot
costs
for
the
smaller
systems
(<
1.0
mgd)
assume
limited
testing
of
the
water
in
an
off­
site
laboratory
or
possibly
at
the
ozone
generation
system
vendor's
facility.
The
cost
for
larger
systems
was
based
on
a
detailed
cost
estimate
of
an
existing
pilot
system.
The
piloting
assumptions
for
the
larger
systems
include
equipment
necessary
to
perform
the
testing
(
using
a
small
clear
polyvinyl
chloride
(
PVC)
contactor),
enough
labor
to
run
the
test
four
different
times
for
a
week
each
time
(
to
capture
seasonal
variability),
and
labor
to
write
up
the
findings
in
the
report.
No
off­
gas
destruction
or
ozone
quenching
is
provided.
The
objective
of
such
a
pilot
test
is
to
develop
design
criteria
for
ozone
dose
and
reactor
sizing.
The
costs
above
do
not
capture
the
effort
required
to
understand
how
ozone
treatment
may
impact
other
plant
unit
processes
or
the
stability
of
the
treated
water
in
the
distribution
system.
Such
a
piloting
effort
for
a
large
treatment
system
would
cost
significantly
more
than
the
numbers
shown
in
Exhibit
4.20.

4.4.4.2
Summary
of
Ozonation
O&
M
Cost
Assumptions
O&
M
costs
include
liquid
oxygen
(
LOX)
(
when
used),
quenching
agent,
part
replacement,
performance
monitoring,
electricity,
and
labor.
Exhibit
4.18
details
the
O&
M
assumptions.
Exhibits
4.19
through
4.21
show
the
O&
M
costs.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
46
Exhibit
4.18:
Ozonation
O&
M
Cost
Assumptions
Cost
Item
Basis
LOX
(
where
used)
$
80/
ton
for
LOX
Quench
(
H2O2)
Chemical
suppliers
contacted
for
chemical
costs.

Part
Replacement
Vendor
provided
estimates
as
a
percentage
of
ozone
equipment
costs.

Electricity
Pumps
and
ozone
generation.
$
0.08/
kWh,
11.3
kWh/
lb
ozone
for
smaller
systems
(<
100
lbs/
day),
includes
generator,
destruct,
and
PSA.
5.2
kWh/
lb
ozone
for
LOX
systems,
includes
generator
and
destruct.

Performance
Monitoring
1
sample/
week/
reactor
for
biological
dissolved
organic
carbon,
$
100/
sample.

pH
reduction
(
when
used)
Assuming
50th
percentile
alkalinity
(
78
mg/
L
as
CaCO3)
and
pH
(
7.7)
from
the
ICR
database,
acid
and
caustic
O&
M
costs
were
estimated.
The
unit
costs
for
chemicals
were
based
on
bulk
shipments
from
chemical
suppliers.

Source:
Section
4.4.3
The
labor
costs
are
a
function
of
the
cost
category
and
the
assumptions
on
the
level
of
effort
for
each
system.
Assumptions
for
systems
at
the
technical
rate
($
24.96)
are
as
follows:

°
3
hr/
week
for
monitoring
plus
4
hr/
month
maintenance
(<
100
mgd
design
flow)

°
6
hr/
week
for
monitoring
plus
8
hr/
month
maintenance
(>
100
mgd
design
flow)

Assumptions
for
systems
at
the
managerial
rate
($
44.91)
are
as
follows:

°
1
hr/
week
(<
100
mgd
design
flow)

°
4
hr/
week
(>
100
mgd
design
flow)
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
47
Design
Flow
(
mgd)
0.091
0.18
0.27
0.36
0.68
1
Average
Flow
(
mgd)
0.025
0.054
0.084
0.11
0.23
0.35
Unit
Capital
Cost
Summary
Total
Unit
Capital
Cost
(
no
pH
adj.)
$
306,733
$
331,732
$
410,701
$
429,873
$
574,835
$
655,369
Indirect
Capital
Costs
(
no
pH
adj.)
$
17,174
$
22,566
$
24,115
$
24,491
$
27,333
$
84,652
Total
Unit
Capital
Cost
(
with
pH
adj.)
$
329,465
$
374,856
$
455,400
$
476,147
$
626,708
$
712,841
Indirect
Capital
Costs
(
with
pH
adj.)
$
39,906
$
65,691
$
68,814
$
70,764
$
79,206
$
142,124
Piloting
$
5,000
$
10,000
$
10,000
$
10,000
$
10,000
$
65,000
Permitting
$
3,475
$
3,710
$
4,639
$
4,865
$
6,570
$
8,561
Land
$
2,316
$
2,473
$
3,093
$
3,243
$
4,380
$
5,707
Operator
Training
$
998
$
998
$
998
$
998
$
998
$
0
Housing
$
5,385
$
5,385
$
5,385
$
5,385
$
5,385
$
5,385
pH
adjustment
(
if
used)
22,732
$
43,124
$
44,699
$
46,274
$
51,873
$
57,472
$
Capital
Cost
Multiplier
$
289,559
$
309,166
$
386,586
$
405,382
$
547,502
$
570,716
Subtotal
Process
Cost
$
115,824
$
123,666
$
154,635
$
162,153
$
219,001
$
285,358
Stainless
pipes,
valves,
ductwork
$
15,076
$
16,241
$
21,391
$
22,498
$
32,006
$
42,079
Ozone
process
E&
I
$
12,061
$
12,993
$
17,113
$
17,999
$
25,605
$
33,663
Off­
Gas
Destruction
$
5,945
$
5,945
$
7,926
$
7,926
$
10,898
$
12,385
Effluent
Ozone
Quench
$
4,924
$
4,924
$
4,924
$
4,924
$
4,924
$
4,924
Ozone
Contactor
$
7,824
$
12,484
$
17,232
$
21,661
$
35,914
$
64,316
Ozone
Generation
System
$
41,612
$
41,612
$
55,483
$
55,483
$
76,289
$
86,692
In­
plant
pumping
$
28,382
$
29,467
$
30,565
$
31,662
$
33,365
$
41,300
Chemical
Storage
$
0
$
0
$
0
$
0
$
0
$
0
Annual
O&
M
Summary
Total
Annual
O&
M
Cost
(
no
pH
adjust.)
$
56,531
$
56,686
$
57,147
$
57,286
$
58,379
$
59,246
Total
Annual
O&
M
Cost
(
with
pH
adjust)
$
57,524
$
58,832
$
60,484
$
61,656
$
67,515
$
73,150
Chemicals
O2
$
0
$
0
$
0
$
0
$
0
$
0
Chemicals
H2O2
$
27
$
58
$
90
$
118
$
248
$
377
Part
Replacement
$
900
$
900
$
1,200
$
1,200
$
1,650
$
1,875
Performance
monitoring
$
10,400
$
10,400
$
10,400
$
10,400
$
10,400
$
10,400
Electricity
$
283
$
407
$
535
$
646
$
1,160
$
1,673
Labor
$
44,921
$
44,921
$
44,921
$
44,921
$
44,921
$
44,921
pH
adjustment
(
when
used)
$
993
$
2,145
$
3,337
$
4,370
$
9,137
$
13,904
Exhibit
4.19:
Ozonation
Cost
Summary
(
0.5
log
Cryptosporidium
Inactivation)

Note:
Design
Dose
=
3.19
mg/
L,
Average
Dose
=
1.78
mg/
L
Source:
Section
4.4.4
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
48
Design
Flow
(
mgd)
1.2
2
3.5
7
17
22
76
210
430
520
Average
Flow
(
mgd)
0.41
0.77
1.4
3
7.8
11
38
120
270
350
Unit
Capital
Cost
Summary
Total
Unit
Capital
Cost
(
no
pH
adj.)
$
748,729
$
1,108,348
$
1,400,987
$
2,039,310
$
3,569,008
$
4,057,564
$
11,437,951
$
23,271,892
$
39,346,816
$
46,476,447
Indirect
Capital
Costs
(
no
pH
adj.)
$
86,929
$
98,134
$
111,037
$
140,057
$
228,868
$
263,844
$
692,903
$
1,599,548
$
2,815,232
$
3,187,929
Total
Unit
Capital
Cost
(
with
pH
adj.)
$
809,700
$
1,183,317
$
1,502,201
$
2,201,764
$
3,906,432
$
4,482,473
$
12,807,698
$
26,986,237
$
46,910,501
$
55,614,862
Indirect
Capital
Costs
(
with
pH
adj.)
$
147,901
$
173,103
$
212,251
$
302,511
$
566,292
$
688,753
$
2,062,650
$
5,313,893
$
10,378,917
$
12,326,344
Piloting
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
Permitting
$
9,927
$
15,153
$
19,349
$
28,489
$
50,102
$
56,906
$
161,176
$
325,085
$
500,000
$
500,000
Land
$
6,618
$
10,102
$
12,899
$
18,993
$
33,401
$
37,937
$
107,450
$
216,723
$
365,316
$
432,885
Operator
Training
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Housing
$
5,385
$
7,879
$
13,788
$
27,576
$
80,365
$
104,001
$
359,277
$
992,740
$
1,884,916
$
2,190,044
pH
adjustment
(
if
used)
60,971
$
74,969
$
101,215
$
162,454
$
337,424
$
424,909
$
1,369,747
$
3,714,345
$
7,563,685
$
9,138,415
$
Capital
Cost
Multiplier
$
661,799
$
1,010,214
$
1,289,950
$
1,899,253
$
3,340,139
$
3,793,720
$
10,745,047
$
21,672,343
$
36,531,584
$
43,288,518
Subtotal
Process
Cost
$
330,900
$
505,107
$
644,975
$
949,626
$
1,670,070
$
1,896,860
$
5,372,524
$
10,836,172
$
18,265,792
$
21,644,259
Stainless
pipes,
valves,
ductwork
$
49,175
$
76,639
$
96,674
$
142,437
$
253,100
$
286,814
$
733,464
$
1,335,796
$
2,059,087
$
2,413,441
Ozone
process
E&
I
$
39,340
$
61,311
$
77,339
$
113,950
$
202,480
$
229,451
$
586,772
$
1,068,637
$
1,647,270
$
1,930,752
Off­
Gas
Destruction
$
14,861
$
24,769
$
28,732
$
39,630
$
69,353
$
74,307
$
208,060
$
326,951
$
416,120
$
475,566
Effluent
Ozone
Quench
$
4,924
$
4,924
$
4,924
$
8,283
$
8,283
$
16,566
$
99,076
$
99,076
$
198,152
$
198,152
Ozone
Contactor
$
72,886
$
103,479
$
151,916
$
244,421
$
449,292
$
536,233
$
1,170,302
$
2,628,498
$
4,709,238
$
5,651,086
Ozone
Generation
System
$
104,030
$
173,383
$
201,125
$
277,413
$
485,473
$
520,150
$
1,456,419
$
2,288,659
$
2,912,839
$
3,328,959
In­
plant
pumping
$
45,683
$
60,601
$
82,590
$
121,187
$
197,985
$
228,337
$
1,103,716
$
3,049,742
$
6,244,710
$
7,551,743
Chemical
Storage
$
0
$
0
$
1,675
$
2,305
$
4,103
$
5,002
$
14,713
$
38,812
$
78,376
$
94,561
Annual
O&
M
Summary
Total
Annual
O&
M
Cost
(
no
pH
adjust.)
$
59,942
$
63,369
$
70,679
$
84,708
$
126,345
$
151,853
$
386,197
$
1,131,923
$
2,326,749
$
2,965,095
Total
Annual
O&
M
Cost
(
with
pH
adjust)
$
76,229
$
93,958
$
126,295
$
203,884
$
436,204
$
588,833
$
1,895,766
$
5,898,984
$
13,052,635
$
16,869,022
Chemicals
O2
$
0
$
0
$
3,338
$
7,152
$
18,596
$
26,226
$
90,597
$
286,097
$
643,718
$
834,449
Chemicals
H2O2
$
441
$
829
$
1,507
$
3,228
$
8,394
$
11,837
$
40,892
$
129,132
$
290,546
$
376,634
Part
Replacement
$
2,250
$
3,750
$
4,350
$
6,000
$
10,500
$
11,250
$
31,500
$
49,500
$
63,000
$
72,000
Performance
monitoring
$
10,400
$
10,400
$
10,400
$
10,400
$
10,400
$
10,400
$
15,600
$
31,200
$
52,000
$
62,400
Electricity
$
1,929
$
3,469
$
6,163
$
13,006
$
33,533
$
47,219
$
162,687
$
513,368
$
1,154,858
$
1,496,986
Labor
$
44,921
$
44,921
$
44,921
$
44,921
$
44,921
$
44,921
$
44,921
$
122,627
$
122,627
$
122,627
pH
adjustment
(
when
used)
$
16,287
$
30,589
$
55,616
$
119,177
$
309,859
$
436,981
$
1,509,569
$
4,767,061
$
10,725,886
$
13,903,927
Exhibit
4.19
(
continued):
Ozonation
Cost
Summary
(
0.5
log
Cryptosporidium
Inactivation)

Note:
Design
Dose
=
3.19
mg/
L,
Average
Dose
=
1.78
mg/
L
Source:
Section
4.4.4
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
49
Design
Flow
(
mgd)
0.091
0.18
0.27
0.36
0.68
1
Average
Flow
(
mgd)
0.025
0.054
0.084
0.11
0.23
0.35
Unit
Capital
Cost
Summary
Total
Unit
Capital
Cost
(
no
pH
adj.)
$
306,733
$
390,345
$
410,701
$
517,793
$
618,795
$
832,071
Indirect
Capital
Costs
(
no
pH
adj.)
$
17,174
$
23,715
$
24,115
$
26,214
$
28,195
$
88,962
Total
Unit
Capital
Cost
(
with
pH
adj.)
$
329,465
$
433,470
$
455,400
$
564,067
$
670,668
$
889,543
Indirect
Capital
Costs
(
with
pH
adj.)
$
39,906
$
66,840
$
68,814
$
72,488
$
80,068
$
146,434
Piloting
$
5,000
$
10,000
$
10,000
$
10,000
$
10,000
$
65,000
Permitting
$
3,475
$
4,400
$
4,639
$
5,899
$
7,087
$
11,147
Land
$
2,316
$
2,933
$
3,093
$
3,933
$
4,725
$
7,431
Operator
Training
$
998
$
998
$
998
$
998
$
998
$
0
Housing
$
5,385
$
5,385
$
5,385
$
5,385
$
5,385
$
5,385
pH
adjustment
(
if
used)
22,732
$
43,124
$
44,699
$
46,274
$
51,873
$
57,472
$
Capital
Cost
Multiplier
$
289,559
$
366,630
$
386,586
$
491,579
$
590,600
$
743,109
Subtotal
Process
Cost
$
115,824
$
146,652
$
154,635
$
196,631
$
236,240
$
371,554
Stainless
pipes,
valves,
ductwork
$
15,076
$
20,204
$
21,391
$
28,443
$
34,978
$
56,940
Ozone
process
E&
I
$
12,061
$
16,163
$
17,113
$
22,754
$
27,983
$
45,552
Off­
Gas
Destruction
$
5,945
$
7,926
$
7,926
$
10,898
$
12,385
$
19,815
Effluent
Ozone
Quench
$
4,924
$
4,924
$
4,924
$
4,924
$
4,924
$
4,924
Ozone
Contactor
$
7,824
$
12,484
$
17,232
$
21,661
$
35,914
$
64,316
Ozone
Generation
System
$
41,612
$
55,483
$
55,483
$
76,289
$
86,692
$
138,707
In­
plant
pumping
$
28,382
$
29,467
$
30,565
$
31,662
$
33,365
$
41,300
Chemical
Storage
$
0
$
0
$
0
$
0
$
0
$
0
Annual
O&
M
Summary
Total
Annual
O&
M
Cost
(
no
pH
adjust.)
$
56,652
$
57,163
$
57,382
$
58,021
$
59,121
$
61,121
Total
Annual
O&
M
Cost
(
with
pH
adjust)
$
57,645
$
59,308
$
60,719
$
62,391
$
68,258
$
75,025
Chemicals
O2
$
0
$
0
$
0
$
0
$
0
$
0
Chemicals
H2O2
$
42
$
90
$
140
$
183
$
382
$
582
Part
Replacement
$
900
$
1,200
$
1,200
$
1,650
$
1,875
$
3,000
Performance
monitoring
$
10,400
$
10,400
$
10,400
$
10,400
$
10,400
$
10,400
Electricity
$
389
$
552
$
721
$
867
$
1,542
$
2,218
Labor
$
44,921
$
44,921
$
44,921
$
44,921
$
44,921
$
44,921
pH
adjustment
(
when
used)
$
993
$
2,145
$
3,337
$
4,370
$
9,137
$
13,904
Exhibit
4.20:
Ozonation
Cost
Summary
(
1.0
log
Cryptosporidium
Inactivation)

Note:
Design
Dose
=
5.00
mg/
L,
Average
Dose
=
2.75
mg/
L
Source:
Section
4.4.4
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
50
Design
Flow
(
mgd)
1.2
2
3.5
7
17
22
76
210
430
520
Average
Flow
(
mgd)
0.41
0.77
1.4
3
7.8
11
38
120
270
350
Unit
Capital
Cost
Summary
Total
Unit
Capital
Cost
(
no
pH
adj.)
$
984,875
$
1,207,059
$
1,560,888
$
2,527,627
$
3,760,584
$
4,474,581
$
12,835,717
$
25,122,969
$
45,090,556
$
52,943,646
Indirect
Capital
Costs
(
no
pH
adj.)
$
93,219
$
104,903
$
122,569
$
167,233
$
278,027
$
331,586
$
925,876
$
2,028,629
$
3,644,229
$
4,204,841
Total
Unit
Capital
Cost
(
with
pH
adj.)
$
1,045,847
$
1,282,028
$
1,662,102
$
2,690,081
$
4,098,008
$
4,899,490
$
14,205,464
$
28,837,314
$
52,654,241
$
62,082,061
Indirect
Capital
Costs
(
with
pH
adj.)
$
154,190
$
179,872
$
223,784
$
329,687
$
615,451
$
756,495
$
2,295,623
$
5,742,974
$
11,207,914
$
13,343,256
Piloting
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
Permitting
$
13,375
$
16,532
$
21,575
$
35,406
$
52,238
$
62,145
$
178,648
$
346,415
$
500,000
$
500,000
Land
$
8,917
$
11,022
$
14,383
$
23,604
$
34,826
$
41,430
$
119,098
$
230,943
$
414,463
$
487,388
Operator
Training
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Housing
$
5,928
$
12,349
$
21,611
$
43,223
$
125,963
$
163,011
$
563,130
$
1,386,271
$
2,664,765
$
3,152,452
pH
adjustment
(
if
used)
60,971
$
74,969
$
101,215
$
162,454
$
337,424
$
424,909
$
1,369,747
$
3,714,345
$
7,563,685
$
9,138,415
$
Capital
Cost
Multiplier
$
891,656
$
1,102,156
$
1,438,318
$
2,360,394
$
3,482,557
$
4,142,995
$
11,909,841
$
23,094,340
$
41,446,328
$
48,738,806
Subtotal
Process
Cost
$
445,828
$
551,078
$
719,159
$
1,180,197
$
1,741,279
$
2,071,497
$
5,954,920
$
11,547,170
$
20,723,164
$
24,369,403
Stainless
pipes,
valves,
ductwork
$
68,991
$
84,565
$
109,403
$
182,067
$
265,079
$
316,537
$
832,541
$
1,454,688
$
2,475,207
$
2,874,145
Ozone
process
E&
I
$
55,192
$
67,652
$
87,522
$
145,654
$
212,063
$
253,229
$
666,033
$
1,163,750
$
1,980,166
$
2,299,316
Off­
Gas
Destruction
$
24,769
$
28,732
$
34,677
$
59,446
$
74,307
$
89,169
$
257,598
$
386,397
$
624,180
$
693,533
Effluent
Ozone
Quench
$
4,924
$
4,924
$
8,283
$
8,283
$
16,566
$
16,566
$
99,076
$
99,076
$
198,152
$
297,228
Ozone
Contactor
$
72,886
$
103,479
$
151,916
$
244,421
$
449,292
$
536,233
$
1,170,302
$
2,628,498
$
4,709,238
$
5,651,086
Ozone
Generation
System
$
173,383
$
201,125
$
242,737
$
416,120
$
520,150
$
624,180
$
1,803,186
$
2,704,779
$
4,369,258
$
4,854,731
In­
plant
pumping
$
45,683
$
60,601
$
82,590
$
121,187
$
197,985
$
228,337
$
1,103,716
$
3,049,742
$
6,244,710
$
7,551,743
Chemical
Storage
$
0
$
0
$
2,032
$
3,019
$
5,838
$
7,247
$
22,468
$
60,240
$
122,252
$
147,621
Annual
O&
M
Summary
Total
Annual
O&
M
Cost
(
no
pH
adjust.)
$
62,308
$
65,533
$
76,182
$
97,490
$
152,412
$
189,778
$
516,761
$
1,529,391
$
3,232,212
$
4,130,989
Total
Annual
O&
M
Cost
(
with
pH
adjust)
$
78,596
$
96,121
$
131,798
$
216,666
$
462,271
$
626,758
$
2,026,330
$
6,296,452
$
13,958,098
$
18,034,916
Chemicals
O2
$
0
$
0
$
5,157
$
11,050
$
28,730
$
40,517
$
139,968
$
442,003
$
994,507
$
1,289,176
Chemicals
H2O2
$
682
$
1,280
$
2,328
$
4,988
$
12,968
$
18,288
$
63,175
$
199,501
$
448,877
$
581,878
Part
Replacement
$
3,750
$
4,350
$
5,250
$
9,000
$
11,250
$
13,500
$
39,000
$
58,500
$
94,500
$
105,000
Performance
monitoring
$
10,400
$
10,400
$
10,400
$
10,400
$
10,400
$
10,400
$
15,600
$
31,200
$
52,000
$
62,400
Electricity
$
2,555
$
4,581
$
8,127
$
17,131
$
44,143
$
62,152
$
214,097
$
675,560
$
1,519,700
$
1,969,908
Labor
$
44,921
$
44,921
$
44,921
$
44,921
$
44,921
$
44,921
$
44,921
$
122,627
$
122,627
$
122,627
pH
adjustment
(
when
used)
$
16,287
$
30,589
$
55,616
$
119,177
$
309,859
$
436,981
$
1,509,569
$
4,767,061
$
10,725,886
$
13,903,927
Exhibit
4.20
(
continued):
Ozonation
Cost
Summary
(
1.0
log
Cryptosporidium
Inactivation)

Note:
Design
Dose
=
5.00
mg/
L,
Average
Dose
=
2.75
mg/
L
Source:
Section
4.4.4
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
June
2003
4­
51
Design
Flow
(
mgd)
0.091
0.18
0.27
0.36
0.68
1
Average
Flow
(
mgd)
0.025
0.054
0.084
0.11
0.23
0.35
Unit
Capital
Cost
Summary
Total
Unit
Capital
Cost
(
no
pH
adj.)
$
365,347
$
390,345
$
498,621
$
561,753
$
838,596
$
951,897
Indirect
Capital
Costs
(
no
pH
adj.)
$
18,323
$
23,715
$
25,839
$
27,076
$
32,505
$
93,861
Total
Unit
Capital
Cost
(
with
pH
adj.)
$
388,078
$
433,470
$
543,320
$
608,027
$
890,468
$
1,009,369
Indirect
Capital
Costs
(
with
pH
adj.)
$
41,055
$
66,840
$
70,538
$
73,350
$
84,378
$
151,333
Piloting
$
5,000
$
10,000
$
10,000
$
10,000
$
10,000
$
65,000
Permitting
$
4,164
$
4,400
$
5,673
$
6,416
$
9,673
$
12,871
Land
$
2,776
$
2,933
$
3,782
$
4,277
$
6,449
$
8,580
Operator
Training
$
998
$
998
$
998
$
998
$
998
$
0
Housing
$
5,385
$
5,385
$
5,385
$
5,385
$
5,385
$
7,410
pH
adjustment
(
if
used)
22,732
$
43,124
$
44,699
$
46,274
$
51,873
$
57,472
$
Capital
Cost
Multiplier
$
347,023
$
366,630
$
472,783
$
534,677
$
806,091
$
858,037
Subtotal
Process
Cost
$
138,809
$
146,652
$
189,113
$
213,871
$
322,436
$
429,018
Stainless
pipes,
valves,
ductwork
$
19,039
$
20,204
$
27,336
$
31,415
$
49,840
$
66,848
Ozone
process
E&
I
$
15,231
$
16,163
$
21,869
$
25,132
$
39,872
$
53,478
Off­
Gas
Destruction
$
7,926
$
7,926
$
10,898
$
12,385
$
19,815
$
24,769
Effluent
Ozone
Quench
$
4,924
$
4,924
$
4,924
$
4,924
$
4,924
$
4,924
Ozone
Contactor
$
7,824
$
12,484
$
17,232
$
21,661
$
35,914
$
64,316
Ozone
Generation
System
$
55,483
$
55,483
$
76,289
$
86,692
$
138,707
$
173,383
In­
plant
pumping
$
28,382
$
29,467
$
30,565
$
31,662
$
33,365
$
41,300
Chemical
Storage
$
0
$
0
$
0
$
0
$
0
$
0
Annual
O&
M
Summary
Total
Annual
O&
M
Cost
(
no
pH
adjust.)
$
57,095
$
57,373
$
58,111
$
58,586
$
60,864
$
62,767
Total
Annual
O&
M
Cost
(
with
pH
adjust)
$
58,088
$
59,518
$
61,448
$
62,956
$
70,001
$
76,671
Chemicals
O2
$
0
$
0
$
0
$
0
$
0
$
0
Chemicals
H2O2
$
59
$
128
$
199
$
260
$
544
$
827
Part
Replacement
$
1,200
$
1,200
$
1,650
$
1,875
$
3,000
$
3,750
Performance
monitoring
$
10,400
$
10,400
$
10,400
$
10,400
$
10,400
$
10,400
Electricity
$
514
$
724
$
941
$
1,130
$
1,999
$
2,868
Labor
$
44,921
$
44,921
$
44,921
$
44,921
$
44,921
$
44,921
pH
adjustment
(
when
used)
$
993
$
2,145
$
3,337
$
4,370
$
9,137
$
13,904
Exhibit
4.21:
Ozonation
Cost
Summary
(
2.0
log
Cryptosporidium
Inactivation)

Note:
Design
Dose
=
7.50
mg/
L,
Average
Dose
=
3.91
mg/
L
Source:
Section
4.4.4
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
June
2003
4­
52
Design
Flow
(
mgd)
1.2
2
3.5
7
17
22
76
210
430
520
Average
Flow
(
mgd)
0.41
0.77
1.4
3
7.8
11
38
120
270
350
Unit
Capital
Cost
Summary
Total
Unit
Capital
Cost
(
no
pH
adj.)
$
1,082,080
$
1,344,897
$
1,784,747
$
2,786,864
$
4,299,684
$
5,176,071
$
14,058,615
$
27,778,067
$
51,856,072
$
60,994,144
Indirect
Capital
Costs
(
no
pH
adj.)
$
98,482
$
114,289
$
138,571
$
194,640
$
352,622
$
428,214
$
1,207,926
$
2,728,216
$
4,944,371
$
5,845,168
Total
Unit
Capital
Cost
(
with
pH
adj.)
$
1,143,052
$
1,419,866
$
1,885,962
$
2,949,318
$
4,637,108
$
5,600,980
$
15,428,362
$
31,492,412
$
59,419,757
$
70,132,559
Indirect
Capital
Costs
(
with
pH
adj.)
$
159,453
$
189,258
$
239,786
$
357,094
$
690,046
$
853,123
$
2,577,673
$
6,442,561
$
12,508,056
$
14,983,583
Piloting
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
$
65,000
Permitting
$
14,754
$
18,459
$
24,693
$
38,883
$
59,206
$
71,218
$
192,760
$
375,748
$
500,000
$
500,000
Land
$
9,836
$
12,306
$
16,462
$
25,922
$
39,471
$
47,479
$
128,507
$
250,499
$
469,117
$
551,490
Operator
Training
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Housing
$
8,892
$
18,524
$
32,417
$
64,834
$
188,945
$
244,517
$
821,658
$
2,036,969
$
3,910,254
$
4,728,679
pH
adjustment
(
if
used)
60,971
$
74,969
$
101,215
$
162,454
$
337,424
$
424,909
$
1,369,747
$
3,714,345
$
7,563,685
$
9,138,415
$
Capital
Cost
Multiplier
$
983,599
$
1,230,608
$
1,646,176
$
2,592,224
$
3,947,062
$
4,747,858
$
12,850,690
$
25,049,851
$
46,911,702
$
55,148,975
Subtotal
Process
Cost
$
491,799
$
615,304
$
823,088
$
1,296,112
$
1,973,531
$
2,373,929
$
6,425,345
$
12,524,926
$
23,455,851
$
27,574,488
Stainless
pipes,
valves,
ductwork
$
76,917
$
95,312
$
127,237
$
201,883
$
304,709
$
368,145
$
911,802
$
1,618,163
$
2,935,911
$
3,414,110
Ozone
process
E&
I
$
61,533
$
76,250
$
101,789
$
161,506
$
243,767
$
294,516
$
729,441
$
1,294,531
$
2,348,729
$
2,731,288
Off­
Gas
Destruction
$
28,732
$
33,686
$
43,594
$
69,353
$
94,122
$
113,938
$
297,228
$
455,750
$
842,147
$
951,131
Effluent
Ozone
Quench
$
4,924
$
8,283
$
8,283
$
8,283
$
16,566
$
24,848
$
99,076
$
198,152
$
297,228
$
396,305
Ozone
Contactor
$
72,886
$
103,479
$
151,916
$
244,421
$
449,292
$
536,233
$
1,170,302
$
2,628,498
$
4,709,238
$
5,651,086
Ozone
Generation
System
$
201,125
$
235,801
$
305,155
$
485,473
$
658,856
$
797,563
$
2,080,599
$
3,190,252
$
5,895,031
$
6,657,917
In­
plant
pumping
$
45,683
$
60,601
$
82,590
$
121,187
$
197,985
$
228,337
$
1,103,716
$
3,049,742
$
6,244,710
$
7,551,743
Chemical
Storage
$
0
$
1,891
$
2,526
$
4,006
$
8,234
$
10,348
$
33,180
$
89,837
$
182,856
$
220,909
Annual
O&
M
Summary
Total
Annual
O&
M
Cost
(
no
pH
adjust.)
$
63,943
$
68,152
$
75,704
$
165,293
$
315,611
$
399,581
$
1,234,372
$
3,485,535
$
7,215,870
$
8,915,410
Total
Annual
O&
M
Cost
(
with
pH
adjust)
$
80,231
$
98,740
$
131,320
$
284,470
$
625,470
$
836,561
$
2,743,942
$
8,252,596
$
17,941,756
$
22,819,337
Chemicals
O2
$
0
$
0
$
0
$
70,319
$
170,774
$
221,002
$
763,460
$
2,109,561
$
4,319,578
$
5,223,676
Chemicals
H2O2
$
969
$
1,820
$
3,309
$
7,091
$
18,438
$
26,002
$
89,824
$
283,654
$
638,222
$
827,324
Part
Replacement
$
4,350
$
5,100
$
6,600
$
10,500
$
14,250
$
17,250
$
45,000
$
69,000
$
127,500
$
144,000
Performance
monitoring
$
10,400
$
10,400
$
10,400
$
10,400
$
10,400
$
10,400
$
15,600
$
31,200
$
52,000
$
62,400
Electricity
$
3,303
$
5,910
$
10,473
$
22,062
$
56,828
$
80,006
$
275,567
$
869,493
$
1,955,943
$
2,535,383
Labor
$
44,921
$
44,921
$
44,921
$
44,921
$
44,921
$
44,921
$
44,921
$
122,627
$
122,627
$
122,627
pH
adjustment
(
when
used)
$
16,287
$
30,589
$
55,616
$
119,177
$
309,859
$
436,981
$
1,509,569
$
4,767,061
$
10,725,886
$
13,903,927
Exhibit
4.21
(
continued):
Ozonation
Cost
Summary
(
2.0
log
Cryptosporidium
Inactivation)

Note:
Design
Dose
=
7.50
mg/
L,
Average
Dose
=
3.91
mg/
L
Source:
Section
4.4.4
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
53
4.4.5
Microfiltration
and
Ultrafiltration
Microfiltration
and
ultrafiltration
can
be
effective
for
the
control
of
microbial
contaminants,
including
Cryptosporidium.
The
costs
presented
in
this
section
assume
an
MF/
UF
system
is
either
an
addition
to
an
existing
conventional
treatment
plant,
or
a
replacement
for
granular
media
filters.
In
the
latter
case,
it
is
assumed
the
settled
water
is
of
sufficient
quality
(
i.
e.,
low
total
suspended
solids)
that
additional
pretreatment
is
not
required.
Costs
are
provided
for
a
design
feed
water
temperature
of
10
°
C.
As
discussed
in
Chapters
2
and
3,
water
temperature
can
impact
system
flux.
The
design
feed
water
temperature
was
selected
as
an
approximate
average
condition
for
systems
that
might
consider
MF/
UF
treatment.
Systems
with
lower
feed
water
temperatures
may
require
additional
membrane
area
or
increased
operating
pressure
to
maintain
the
desired
level
of
production.
Systems
with
warmer
feed
water
temperatures
may
require
smaller
membrane
areas
and
lower
operating
pressures.

MF/
UF
processes
will
generate
a
liquid
residual
stream
that
must
be
disposed
of
or
recycled.
For
the
purposes
of
this
document,
it
was
assumed
that
backwash
and
reject
water
would
be
discharged
to
a
sanitary
sewer
for
treatment
at
a
POTW.
The
costs
presented
assume
an
average
system
recovery
of
93
percent
(
i.
e.,
the
residuals
volume
equals
seven
percent
of
the
average
daily
plant
flow).

4.4.5.1
Summary
of
MF/
UF
Capital
Cost
Assumptions
Process
Costs
Capital
costs
were
estimated
based
on
vendor
data,
cost
estimating
guides
(
RS
Means),
and
best
professional
judgment.
Process
costs
were
obtained
in
2002
adjusted
to
year
2000
dollars
using
the
ENR
BCI.
Exhibit
4.29
presents
a
summary
of
line
item
capital
costs
for
MF/
UF,
based
on
a
design
flow
of
10
°
C,
and
assuming
discharge
of
backwash
water
to
a
sanitary
sewer
for
treatment
at
a
POTW.
This
section
discusses
the
methodology
used
for
estimating
capital
costs.

Membrane
System
For
a
range
of
flows,
vendors
were
asked
to
provide
costs
for
skid­
mounted
membrane
modules
that
included
prefilters
(
about
200
micron),
associated
piping,
feed
pumps,
backwash
and
recirculation
pumps
(
where
appropriate),
chemical
cleaning
feed
tanks
and
pumps,
and
direct
integrity
testing
instrumentation.
A
maximum
skid
size
of
2
mgd
was
required.
Exhibit
4.22
plots
the
cost
estimates
received
from
the
vendors
for
different
design
flows,
as
well
as
the
resulting
cost
equations
that
are
used
to
estimate
membrane
system
costs.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
54
y
=
687557x0.4839
for
x
<
1
mgd
y
=
480429x0.8938
for
x
>
10
mgd
y
=
341615x
+
345942
for
1
<
x
<
10
mgd
$
10,000
$
100,000
$
1,000,000
$
10,000,000
$
100,000,000
$
1,000,000,000
0.01
0.1
1
10
100
1000
Design
Flow
(
mgd)
Capital
Cost
($)
Exhibit
4.22:
Summary
of
MF/
UF
Vendor
Estimates
Source:
Vendor
quotes
Interstage
Piping
and
Pumping
The
costs
associated
with
interstage
pumping
are
included
as
a
process
cost
based
on
the
assumption
that
some
systems
may
not
be
able
to
incorporate
MF/
UF
into
the
existing
plant
hydraulic
profile.
Depending
on
the
system
size,
the
additional
total
dynamic
head
requirements
were
assumed
to
vary
because
of
the
increased
complexities
of
the
larger
systems
(
e.
g.,
additional
pipes,
valves,
and
fittings,
and
more
membrane
skids).
For
the
purposes
of
estimating
a
typical
MF/
UF
system
cost,
TDH
needs
for
systems
were
assumed
to
vary
between
30
and
75
feet
as
shown
in
Exhibit
4.23.
These
assumptions
are
based
on
experience
with
similar
systems.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
55
Exhibit
4.23:
Summary
of
MF/
UF
Interstage
Pumping
Assumptions
System
Size
(
mgd)
Interstage
Pumping
Requirements
(
TDH)*

<
1
30
feet
1
­
10
50
feet
>
10
75
feet
*
Total
Dynamic
Head
Costs
for
interstage
piping
and
pumping
were
estimated
based
upon
vendor
data
and
RS
Means
(
1999).
Pump
and
piping
costs
were
totaled
and
a
regression
line
was
fit
through
the
data
to
estimate
the
costs
for
each
of
the
required
flow
categories.
The
resulting
equations
are
presented
below.

For
design
flow
<
1
mgd:
Interstage
pumps
and
piping
($)
=
28023
×
(
Design
Flow)
0.7265
For
design
flow
>
1
mgd:
Interstage
pumps
and
piping
($)
=
30918
×
(
Design
Flow)
0.8103
An
additional
20
percent
was
added
for
the
cost
of
electrical
and
instrumentation
associated
with
the
interstage
pumping.

Process
Monitoring
Equipment
Membrane
skids
are
generally
equipped
to
conduct
periodic,
direct
integrity
tests
(
e.
g.,
pressure­
hold
test
or
bubble­
point
test).
While
these
methods
are
the
most
sensitive
to
breaches
in
membrane
integrity,
they
do
not
provide
a
real­
time
measure
of
membrane
integrity
(
USEPA
2001).
As
a
result,
on­
line
integrity
testing
may
be
required
for
use
of
MF/
UF
to
remove
microbial
contaminants.
Accordingly,
one
turbidimeter
($
2,500
each)
was
assumed
per
skid
for
systems
less
than
1
mgd,
and
one
particle
counter
($
5,000
each)
was
assumed
per
skid
for
systems
larger
than
1
mgd.
(
A
maximum
skid
size
of
2
mgd
was
assumed
for
all
system
sizes.)

Membrane
I&
C
Costs
for
membrane
system
I&
C
were
estimated
based
upon
vendor
data
and
input
from
industry
experts.
For
systems
less
than
1
mgd,
membrane
I&
C
was
included
in
the
cost
of
the
membrane
system.
For
systems
larger
than
1
mgd,
the
cost
of
membrane
I&
C
was
assumed
to
be
$
100,000
for
the
first
skid
and
$
75,000
for
each
additional
skid.
These
costs
include
interconnection
between
skids
and
tie­
in
to
existing
plant
control
(
e.
g.,
SCADA)
systems.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
56
Capital
Cost
Multipliers
The
capital
costs
previously
discussed
(
membrane
system,
interstage
pumping
and
piping,
membrane
E&
I,
and
process
monitoring
equipment)
were
totaled
to
arrive
at
a
total
process
cost,
and
multiplied
by
a
capital
cost
factor
of
1.67
(
for
flow
<
2
mgd)
or
2.0
(
for
flow
>
2
mgd).
The
result
of
this
multiplication
was
then
added
to
the
indirect
capital
costs
(
discussed
later
in
this
section)
to
arrive
at
the
total
capital
cost.
The
capital
cost
factors
were
intended
to
account
for
items
not
included
in
vendor
estimates.
A
complete
discussion
of
capital
cost
factors,
including
the
components,
is
presented
in
section
4.2.1.

Indirect
Capital
Costs
The
total
permitting,
piloting,
membrane
housing,
land,
operator
training,
and
backwash
pipeline
costs
are
referred
to
as
indirect
capital
costs
for
the
purposes
of
this
document.

Permitting
Significant
process
improvements
will
likely
require
coordination
with
the
appropriate
regulatory
agency.
As
such,
permitting
costs
were
included
at
three
percent
of
the
process
cost.
A
minimum
permitting
fee
of
$
2,500
and
a
maximum
of
$
500,000
was
assumed.

Pilot
Testing
It
was
assumed
that
pilot­
or
bench­
scale
tests
would
be
necessary
to
ensure
compatibility
of
membrane
materials
with
process
chemicals
(
e.
g.,
coagulants
or
polymers),
as
well
as
to
determine
critical
design
parameters,
such
as
design
flux.
Bench­
scale
flat
sheet
tests
were
assumed
for
systems
less
than
0.1
mgd,
at
a
cost
of
$
1,000.
Single­
element
tests
($
10,000)
were
assumed
for
systems
between
0.1
and
1
mgd,
and
three­
month
pilot
tests
were
assumed
for
systems
larger
than
1
mgd
($
60,000).

Membrane
Housing
Membrane
housing
costs
include
the
cost
for
a
building
to
house
the
membrane
skids
and
any
associated
appurtenances
(
e.
g.,
building
electrical,
HVAC,
and
lighting).
For
this
document,
size
was
based
on
an
industry
rule
of
thumb
for
MF/
UF
processes:
1,100
ft2
per
mgd
for
systems
with
design
flows
less
than
10
mgd
and
1,300
ft2
per
mgd
for
design
flows
greater
than
10
mgd.
A
minimum
size
of
200
ft2
was
also
assumed.
The
footprint
was
multiplied
by
a
housing
unit
cost
of
$
48.95,
based
on
RS
Means
values
for
a
factory
type
building.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
57
Land
MF/
UF
requires
significantly
larger
footprints
than
other
technologies
for
which
costs
are
provided.
MF/
UF
is
also
likely
to
be
able
to
be
incorporated
into
existing
process
footprints.
Land
cost
assumptions
for
MF/
UF
are
listed
in
Exhibit
4.24.

Exhibit
4.24:
MF/
UF
Land
Cost
Assumptions
Design
Flow
(
mgd)
Land
Cost
(%
of
Capital)*

<
10
1%

>
10
0.5%
Note:
*
Capital
=
Total
Process
Cost
×
Capital
Cost
Multiplier
Source:
Exhibit
4.7
As
discussed
in
section
4.2.4,
the
NDWAC
cost
working
group
recommended
a
factor
of
two
to
five
percent
for
land.
Previous
technology
cost
efforts
(
USEPA
2001)
adopted
land
costs
at
factor
of
five
percent
for
systems
less
than
1
mgd
and
2
percent
for
systems
greater
than
1
mgd;
however,
previous
cases
assumed
new
plant
construction,
as
opposed
to
a
retrofit
as
was
assumed
in
this
document.
To
measure
the
appropriateness
of
the
NDWAC
recommendations,
an
analysis
of
the
land
cost
(
per
acre)
was
conducted
based
upon
the
footprint
of
the
MF/
UF
process.
The
land
cost
(
as
a
percent
of
capital)
was
adjusted
based
upon
this
analysis
and
best
professional
judgment.
A
list
of
assumptions
used
in
this
analysis
is
listed
below.

°
Minimum
land
purchase
­
0.5
acres
°
Building
area
­
1300
ft2
per
mgd
for
systems
<
10
mgd
­
1100
ft2
per
mgd
for
systems
>
10
mgd
°
Building
is
square
°
50­
foot
perimeter
around
building
The
land
area
was
compared
to
the
land
costs
at
various
percentages,
and
a
"
reasonableness"
valuation
was
made
based
on
best
professional
judgment.
Under
the
final
scenario,
estimates
of
land
costs
gradually
increased
from
$
2,200
per
acre
for
the
smallest
system
size
to
$
92,500
per
acre
for
the
largest.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
58
Operator
Training
The
NDWAC
cost
working
group
also
recommended
inclusion
of
operator
training.
Based
upon
system
size,
this
training
could
last
a
few
hours
or
a
few
days.
Exhibit
4.25
summarizes
the
operator
training
cost
assumptions
used
in
this
document.
Costs
are
based
on
experience
with
similar
systems
and
best
professional
judgement.

Exhibit
4.25:
Summary
of
MF/
UF
Operator
Training
Assumptions
Design
Flow
(
mgd)
Training
Cost
($)

<
0.5
included
in
membrane
system
price
0.5
­
1
$
1,000
1
­
10
$
3,000
10
­
100
$
10,000
>
100
$
25,000
Backwash
Pipeline
Capital
costs
for
a
500­
foot
pipeline
to
discharge
backwash
and
reject
water
to
a
sanitary
sewer
were
estimated
based
on
cost
equations
presented
in
Small
Water
System
Byproducts
Treatment
and
Disposal
Cost
Document
(
DPRA
1993a)
and
Water
System
Byproducts
Treatment
and
Disposal
Cost
Document
(
DPRA
1993b).
These
costs
are
shown
as
an
indirect
cost
(
after
the
application
of
the
capital
cost
multiplier)
because
they
already
include
factors
for
engineering,
contractor
overhead
and
profit,
and
installation.

Exhibit
4.26
summarizes
the
pipe
diameter
assumptions
used
in
the
DPRA
documents.
The
equations
used
to
estimate
pipeline
costs
follow
the
exhibit.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
59
Exhibit
4.26:
Summary
of
Backwash
Disposal
Pipeline
Assumptions
Backwash
Volume
(
mgd)
Pipeline
Diameter
(
inches)
Pipe
Material
<
162,500
2
Sch­
40
PVC
162,500
­
500,000
3
Sch­
40
PVC
500,000
­
750,000
4
Sch­
40
PVC
750,000
­
10,000,000
6
Sch­
40
PVC
10,000,000
­
25,000,000
24
Reinforced
concrete
>
25,000,000
36
Reinforced
concrete
Source:
DPRA
(
1993a
and
1993b).

For
systems
<
1
mgd
(
DPRA
1993a)
Backwash
volume
<
150,000
gpd:
Pipeline
cost
($)
=
3,500
Backwash
volume
>
150,000
gpd:
Pipeline
cost
($)
=
27,000
+
(
3.1
×
(
Backwash
Volume)
0.5)

For
systems
>
1
mgd
(
DPRA
1993b)
Backwash
volume
<
150,000
gpd:
Pipeline
cost
($)
=
4,500
Backwash
volume
>
150,000
gpd:
Pipeline
cost
($)
=
4,600
+
(
0.0019
×
Backwash
Volume)

Costs
in
the
DPRA
documents
are
presented
in
year
1992
dollars.
The
ENR
BCI
(
average
1992
value
=
$
2,834)
was
used
to
escalate
costs
to
June
2001
(
index
=
3,572).
Consequently,
the
results
of
the
previous
equations
were
multiplied
by
a
factor
of
1.26
(
3,572
÷
2,834)
to
obtain
the
final
pipeline
cost
estimates.

4.4.5.2
Summary
of
MF/
UF
O&
M
Cost
Assumptions
MF/
UF
operations
and
maintenance
costs
were
based
on
vendor
estimates,
industry
guidelines,
and
cost
models.
Exhibit
4.28
presents
a
summary
of
line
item
O&
M
costs.
This
section
discusses
the
assumptions
regarding
O&
M
estimates
presented
in
this
document.

Membrane
Replacement
Membrane
replacement
costs
for
all
flows
were
derived
from
typical,
or
average,
replacement
cost
estimates
provided
by
manufacturers.
The
manufacturer
estimates
as
shown
in
Exhibit
4.27
were
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
60
plotted
and
liner
regressions
were
used
to
develop
the
following
best
fit
equation
for
the
full
range
of
design
flows:

Membrane
replacement
($/
yr)
=
(
0.5647
×
Design
Flow2)
+
(
13,152
×
Design
Flow)
+
304.49
Exhibit
4.27:
Summary
of
Membrane
Replacement
Costs
Design
Flow
(
mgd)
Average
Membrane
Replacement
Cost
($/
year)

0.01
$
300
0.1
$
1200
1
$
12,000
10
$
134,400
50
$
672,000
430
$
5,760,000
Source:
Vendor
estimates
Performance
Monitoring
In
addition
to
continuous
turbidity
or
particle
count
monitoring
(
included
in
the
process
monitoring
equipment
line
item),
the
costs
for
periodic
HPC
monitoring
were
included
in
the
O&
M
estimates.
HPC
is
monitored
to
detect
biological
activity
on
the
finished
water
side
of
the
membrane.
HPC
tests
are
available
for
approximately
$
1
per
test,
and
require
one
hour
of
labor.
Thus,
the
cost
per
test
is
$
25.96
($
1
for
materials,
$
24.96
for
one
hour
of
labor).
One
test
per
membrane
skid
per
week
was
assumed.

Clean­
in­
Place
Chemicals
MF/
UF
systems
will
require
periodic
(
typically,
quarterly
or
semi­
annually)
chemical
cleaning
to
remove
biological
and
colloidal
foulants.
This
is
referred
to
as
a
clean­
in­
place
(
CIP)
operation.
CIP
practices
can
include
the
use
of
detergents,
acids,
bases,
oxidizing
agents
(
e.
g.,
chlorine
for
removal
of
biofilm),
chelating
agents,
or
enzymatic
cleaners.
Because
of
the
variability
in
CIP
practices,
a
standard
rule­
of­
thumb
of
$
0.01
per
1000
gallons
of
water
produced
was
applied
to
estimate
CIP
chemical
costs.
Thus,
CIP
chemical
costs
can
be
estimated
as
follows:

CIP
chemicals
($/
yr)
=
0.01
×
Average
Flow
(
mgd)
×
1000
×
365
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
61
Materials
Materials
include
replacement
parts
for
interstage
piping
and
pumping
and
were
estimated
based
on
output
from
the
Water
and
W/
W
Cost
models.
The
resulting
material
cost
equations
are
presented
below:

For
average
flow
<
0.35
mgd
Materials
($/
yr)
=
(­
283.6
×
Average
Flow2)
+
(
283.77
×
Average
Flow)
+
107.62
For
average
flow
0.35
to
4.5
mgd
Materials
($/
yr)
=
(
547.62
×
Average
Flow)
­
24.122
For
average
flow
>
4.5
mgd
Materials
($/
yr)
=
(­
0.3794
×
Average
Flow2)
+
(
394.56
×
Average
Flow)
+
672.35
Power
Power
costs
include
electricity
for
interstage
pumps,
membrane
skids,
and
instrumentation.
Interstage
pumping
power
costs
were
estimated
based
on
annual
kWh
estimates
provided
by
the
Water
and
W/
W
Cost
models
and
membrane
skid
power
requirements
provided
by
vendors.
The
equations
used
for
annual
power
costs
are
provided
below.

For
average
flow
<
0.36
mgd:
Power
($/
yr)
=
16561
×
(
Average
Flow)
1.0113
For
average
flow
0.36
­
4.5
mgd:
Power
($/
yr)
=
(
5096.5
×
Average
Flow)
+
4058.8
For
average
flow
>
4.5
mgd:
Power
($/
yr)
=
(
5356.9
×
Average
Flow)
+
2666.3
Labor
Labor
estimates
include
operation
and
maintenance
of
interstage
pumping
and
membrane
skids,
as
well
as
labor
associated
with
repair
of
process
equipment.
A
technical
labor
rate
of
$
24.96
per
hour
was
assumed
for
all
system
sizes.
Labor
hours
are
based
on
vendor
estimates
and
experience
with
similar
systems.
No
additional
managerial
labor
was
assumed.
A
summary
of
labor
hour
assumptions
is
provided
in
Exhibit
4.28.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
62
Exhibit
4.28:
Summary
of
MF/
UF
Labor
Assumptions
System
Size
(
mgd)
Technical
Labor
(
hrs/
week)

<
0.1
4
0.1
­
1
12
1
­
5
24
5
­
10
40
10
­
100
80
>
100
160
POTW
Surcharge
The
reject
and
backwash
volume
is
assumed
to
be
at
a
volume
of
seven
percent
of
the
feed
flow
(
i.
e.,
93
percent
recovery).
The
discharge
of
reject
and
backwash
water
to
a
POTW
assumed
the
following
(
DPRA
1993):

°
POTW
surcharge
of
$
0.00183/
1,000
gallons
discharged
°
Base
charge
of
$
375/
year
for
small
systems,
$
1,000/
year
for
large
systems
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
63
Design
Flow
0.007
0.022
0.037
0.091
0.18
0.27
0.36
0.68
1
Average
Flow
0.0015
0.0054
0.0095
0.025
0.054
0.084
0.11
0.23
0.35
Unit
Capital
Cost
Summary
Total
Unit
Capital
Cost
$
126,730
$
206,121
$
260,157
$
393,517
$
605,175
$
720,600
$
818,777
$
1,089,993
$
1,533,916
Indirect
Capital
Costs
$
18,712
$
20,327
$
21,797
$
25,425
$
92,318
$
95,458
$
99,102
$
106,480
$
170,348
Membrane
housing
$
9,790
$
9,790
$
9,790
$
9,790
$
63,635
$
63,635
$
63,635
$
63,635
$
63,635
Bench/
pilot­
scale
testing
$
1,000
$
1,000
$
1,000
$
1,000
$
10,000
$
10,000
$
10,000
$
10,000
$
60,000
Permitting
$
2,500
$
3,338
$
4,282
$
6,612
$
9,213
$
11,230
$
12,928
$
17,668
$
24,495
Land
$
1,080
$
1,858
$
2,384
$
3,681
$
5,129
$
6,251
$
7,197
$
9,835
$
13,636
Operator
Training
$
1,000
$
1,000
$
3,000
500'
backwash
discharge
pipeline
$
4,342
$
4,342
$
4,342
$
4,342
$
4,342
$
4,342
$
4,342
$
4,342
$
5,582
Capital
Cost
Multiplier
$
108,019
$
185,794
$
238,360
$
368,092
$
512,857
$
625,142
$
719,676
$
983,514
$
1,363,568
Subtotal
Process
Cost
$
64,682
$
111,254
$
142,730
$
220,415
$
307,100
$
374,336
$
430,943
$
588,930
$
816,508
Interstage
piping
and
pumping
$
750
$
1,723
$
2,514
$
4,834
$
7,935
$
10,653
$
13,129
$
20,840
$
30,428
Membrane
equipment
$
61,321
$
106,725
$
137,253
$
212,153
$
295,118
$
359,093
$
412,728
$
561,462
$
676,659
Process
monitoring
equipment
$
2,460
$
2,460
$
2,460
$
2,460
$
2,460
$
2,460
$
2,460
$
2,460
$
4,921
Electrical
$
150
$
345
$
503
$
967
$
1,587
$
2,131
$
2,626
$
4,168
$
6,086
I&
C
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
0
$
98,415
Annual
O&
M
Summary
Total
Annual
O&
M
Cost
$
7,145
$
7,601
$
8,071
$
9,815
$
23,306
$
26,497
$
29,421
$
41,671
$
69,500
Membrane
Replacement
$
397
$
594
$
791
$
1,501
$
2,672
$
3,856
$
5,039
$
9,248
$
13,457
Performance
monitoring
$
1,350
$
1,350
$
1,350
$
1,350
$
1,350
$
1,350
$
1,350
$
1,350
$
1,350
CIP
Chemicals
$
5
$
20
$
35
$
91
$
197
$
307
$
402
$
840
$
1,278
Materials
$
108
$
109
$
110
$
115
$
122
$
129
$
135
$
158
$
172
Electricity
$
23
$
84
$
149
$
397
$
865
$
1,353
$
1,777
$
3,746
$
5,728
Technical
Labor
$
5,192
$
5,192
$
5,192
$
5,192
$
15,575
$
15,575
$
15,575
$
15,575
$
31,150
Managerial
labor
POTW
surcharge
$
70
$
252
$
444
$
1,169
$
2,525
$
3,928
$
5,143
$
10,754
$
16,365
Exhibit
4.29:
Microfiltration/
Ultrafiltration
Cost
Summary
Note:
Based
on
Temperature=
10
°
C
Assume
discharge
to
sanitary
sewer
Source:
Section
4.4.5
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
64
Design
Flow
1.2
2
3.5
7
17
22
76
210
430
520
Average
Flow
0.41
0.77
1.4
3
7.8
11
38
120
270
350
Unit
Capital
Cost
Summary
Total
Unit
Capital
Cost
$
1,672,053
$
2,615,310
$
3,981,989
$
7,095,991
$
15,365,946
$
19,274,465
$
58,795,535
$
147,293,783
$
282,503,048
$
335,884,024
Indirect
Capital
Costs
$
186,486
$
254,863
$
382,005
$
675,810
$
1,275,681
$
1,617,073
$
4,949,693
$
12,606,239
$
25,102,001
$
30,204,293
Membrane
housing
$
76,362
$
127,270
$
222,723
$
445,445
$
915,365
$
1,184,590
$
4,092,220
$
11,307,450
$
23,153,350
$
27,999,400
Bench/
pilot­
scale
testing
$
60,000
$
60,000
$
60,000
$
60,000
$
60,000
$
60,000
$
60,000
$
60,000
$
60,000
$
60,000
Permitting
$
26,687
$
35,407
$
54,000
$
96,303
$
211,354
$
264,861
$
500,000
$
500,000
$
500,000
$
500,000
Land
$
14,856
$
23,604
$
36,000
$
64,202
$
70,451
$
88,287
$
269,229
$
673,438
$
1,287,005
$
1,528,399
Operator
Training
$
3,000
$
3,000
$
3,000
$
3,000
$
10,000
$
10,000
$
10,000
$
25,000
$
25,000
$
25,000
500'
backwash
discharge
pipeline
$
5,582
$
5,582
$
6,283
$
6,861
$
8,511
$
9,335
$
18,244
$
40,351
$
76,646
$
91,494
Capital
Cost
Multiplier
$
1,485,567
$
2,360,447
$
3,599,984
$
6,420,181
$
14,090,265
$
17,657,392
$
53,845,841
$
134,687,544
$
257,401,046
$
305,679,731
Subtotal
Process
Cost
$
889,561
$
1,180,224
$
1,799,992
$
3,210,090
$
7,045,133
$
8,828,696
$
26,922,921
$
67,343,772
$
128,700,523
$
152,839,865
Interstage
piping
and
pumping
$
35,272
$
53,358
$
83,971
$
147,250
$
302,207
$
372,424
$
1,016,940
$
2,317,216
$
4,141,634
$
4,831,142
Membrane
equipment
$
743,899
$
1,012,859
$
1,517,159
$
2,693,859
$
5,949,293
$
7,491,133
$
22,686,175
$
56,271,657
$
106,778,594
$
126,547,591
Process
monitoring
equipment
$
4,921
$
4,921
$
9,841
$
19,683
$
44,287
$
54,128
$
186,988
$
516,678
$
1,057,960
$
1,279,394
Electrical
$
7,054
$
10,672
$
16,794
$
29,450
$
60,441
$
74,485
$
203,388
$
463,443
$
828,327
$
966,228
I&
C
$
98,415
$
98,415
$
172,226
$
319,848
$
688,904
$
836,527
$
2,829,429
$
7,774,778
$
15,894,007
$
19,215,510
Annual
O&
M
Summary
Total
Annual
O&
M
Cost
$
75,603
$
106,304
$
162,699
$
321,899
$
781,382
$
1,029,635
$
3,295,042
$
9,873,367
$
21,396,307
$
27,162,834
Membrane
Replacement
$
16,088
$
26,611
$
46,343
$
92,396
$
224,052
$
289,922
$
1,003,118
$
2,787,128
$
5,760,078
$
6,992,039
Performance
monitoring
$
1,350
$
1,350
$
2,700
$
5,400
$
12,149
$
14,849
$
51,297
$
141,742
$
290,233
$
350,979
CIP
Chemicals
$
1,497
$
2,811
$
5,110
$
10,950
$
28,470
$
40,150
$
138,700
$
438,000
$
985,500
$
1,277,500
Materials
$
200
$
398
$
743
$
1,619
$
3,727
$
4,967
$
15,118
$
42,556
$
79,545
$
92,292
Electricity
$
6,148
$
7,983
$
11,194
$
19,348
$
44,450
$
61,592
$
206,229
$
645,494
$
1,449,029
$
1,877,581
Technical
Labor
$
31,150
$
31,150
$
31,150
$
51,917
$
103,834
$
103,834
$
103,834
$
207,667
$
207,667
$
207,667
Managerial
labor
POTW
surcharge
$
19,170
$
36,003
$
65,459
$
140,270
$
364,701
$
514,322
$
1,776,747
$
5,610,780
$
12,624,255
$
16,364,775
Exhibit
4.29
(
continued):
Microfiltration/
Ultrafiltration
Cost
Summary
Note:
Based
on
Temperature=
10
°
C
Assume
discharge
to
sanitary
sewer
Source:
Section
4.4.5
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
65
4.4.6
Bag
and
Cartridge
Filtration
The
costs
presented
in
this
section
assume
installation
of
bag
or
cartridge
filters
following
conventional
treatment
(
i.
e.,
granular
media
filtration).
This
level
of
pre­
treatment
reduces
the
suspended
solids
concentration
delivered
to
the
filters,
which
in
turn
allows
for
longer
run
times
and
reduced
maintenance
demands.
As
a
result,
costs
for
installation
of
bag
or
cartridge
filters
as
the
sole
treatment
technology
may
be
different
than
those
presented
here.

Costs
for
bag
and
cartridge
filters
were
only
estimated
for
systems
with
a
design
flow
of
2
mgd
or
less.
These
technologies
are
not
typically
used
in
large
systems
due
to
poor
economies
of
scale
and
difficulties
with
design
for
high
flow
rates.

4.4.6.1
Summary
of
Bag
and
Cartridge
Filter
Capital
Cost
Assumptions
Process
Costs
Capital
costs
for
bag
and
cartridge
filters
were
estimated
using
vendor
quotes
and
cost
estimating
guides
(
RS
Means).
Vendor
quotes
were
received
in
July
2002
and
adjusted
to
year
2000
dollars
using
the
ENR
BCI.
Bag
and
cartridge
filter
vendors
were
screened
based
on
anticipated
Cryptosporidium
removal
credits
granted
under
the
LT2ESWTR
and
on
demonstrated
Cryptosporidium
removal
efficiency.
Bag
filters
are
eligible
for
up
to
l
log
removal
credit
and
must
have
been
capable
of
1.5
log
removal
(
includes
0.5­
log
safety
factor).
Cartridge
filters
are
eligible
for
up
to
2
log
removal
credit
and
must
have
been
capable
of
2.5
log
removal
(
includes
0.5
log
safety
factor).
Two
bag
filter
and
three
cartridge
filter
vendors
were
identified
that
met
these
criteria.
Exhibits
4.32
and
4.33
present
line
item
summaries
of
capital
costs
for
bag
and
cartridge
filters.
This
section
presents
the
methodology
by
which
line
item
costs
are
estimated.

Filter
Housing
Estimates
for
bag
and
cartridge
filter
housing
were
estimated
based
on
quotes
provided
by
vendors.
Vendors
provided
estimates
for
stainless
steel
filter
housing
at
each
of
the
flows
for
which
costs
were
provided.
Vendor
quotations
were
averaged
at
each
flow
to
develop
estimates
for
filter
housing
costs.

Initial
Bag
and
Cartridge
Filters
The
initial
cost
of
bag
and
cartridge
filters
was
estimated
using
vendor
quotes.
As
previously
mentioned,
vendors
were
pre­
screened
based
on
demonstrated
Cryptosporidium
removal
efficiency.
Vendors
provided
estimates
for
a
variety
of
bag
and
cartridge
types
and
sizes.
Exhibit
4.30
is
a
summary
of
the
design
criteria
provided
by
the
vendors
for
bag
and
cartridge
filtration.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
66
Exhibit
4.30:
Design
Criteria
for
Bag
and
Cartridge
Filters
Criteria
Bag
Filters
Cartridge
Filters
Nominal
Pore
Size
1
micron
1
micron
Material
polyester
or
polypropylene
pleated
polyester,
pleated
polypropylene,
spun
bonded
polypropylene,
and
absolute
rated
polypropylene
Dimensions
7
inches
by
16
inches,
and
7
inches
by
32
inches
1
inch
ID
by
2.5
inches
OD,
lengths
of
10,
20,
and
30
inches
Housing
Construction
304
Stainless
Steel
304
Stainless
Steel
Loading
Rate
45
gpm
per
16
inches
equivalent
length
10
gpm
(
pleated
construction
only),
5
gpm
per
10
inches
equivalent
length
Source:
Vendor
quotes
Vendors
provided
estimates
at
each
of
the
flows
for
which
costs
are
provided.
Vendor
quotations
were
averaged
at
each
flow
to
develop
the
estimates
for
initial
bags
or
cartridges.

Interstage
Pumping
Costs
for
centrifugal
in­
line
vertical­
mount
single­
stage
pumps
were
estimated
using
RS
Means
(
1999).
A
summary
of
the
data
used
for
estimating
the
line
item
cost
for
pumping
is
presented
in
Exhibit
4.31.
The
resulting
equation
is
listed
here.

Interstage
pumping
($)
=
(­
2,245.4
×
Design
Flow2)
+
(
8,127.7
×
Design
Flow)
+
149.26
Exhibit
4.31:
Summary
of
Bag
and
Cartridge
Filter
Pump
Cost
Data
Design
Flow
(
mgd)
Max
Pumping
Rate
(
gpm)
Pump
Rating
(
Hp)
Pump
Cost
($)

0.024
50
3
$
445
0.087
75
5
$
755
0.27
200
7.5
$
2,125
0.65
750
25
$
4,525
1.8
1500
50
$
7,500
Source:
RS
means
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
67
Instrumentation
and
Controls,
Pipes
and
Valves
Estimates
for
P&
V
and
I&
C,
which
primarily
include
tie­
ins
to
existing
electrical
and
pressure
gauges,
were
based
on
vendor
estimates.
Vendors
provided
estimates
for
these
items
at
each
of
the
flows
for
which
costs
were
provided.
The
quotations
were
averaged
at
each
flow
to
estimate
the
costs
presented
in
Exhibits
4.32
and
4.33.

Capital
Cost
Multipliers
Filter
housing,
initial
filters,
pumps,
electrical,
and
P&
V
were
totaled
to
arrive
at
the
total
process
cost.
For
systems
treating
less
than
2
mgd,
the
process
cost
was
multiplied
by
a
capital
cost
factor
of
1.2,
assuming
that
these
are
package
systems
which
only
require
an
installation
cost.
A
capital
cost
factor
of
1.67
was
used
for
the
2
mgd
systems.

Indirect
Capital
Costs
Indirect
capital
costs
include
permitting,
operator
training,
and
housing.
Permitting
fees
were
estimated
at
$
2,500
for
all
system
sizes.
Operator
training
was
assumed
to
be
$
500
for
all
system
sizes.

Housing
represents
the
cost
associated
with
a
building
for
the
bag
or
cartridge
filters.
Many
facilities
may
be
able
to
incorporate
these
systems
into
the
existing
plant
footprint.
However,
it
was
assumed
that,
in
half
or
more
cases,
this
would
not
be
possible.
In
such
cases,
bag
or
cartridge
filters
would
be
installed
near
the
plant
high­
service
pump
station,
which
may
not
have
sufficient
space
available
to
accommodate
these
processes.
Based
on
housing
area
requirements
for
membrane
processes
(
e.
g.,
1,300
ft2
per
mgd
for
MF/
UF
less
than
10
mgd),
a
housing
area
of
500
ft2
per
mgd
was
assumed.
This
was
based
on
best
professional
judgment
as
to
the
relative
size
of
bag
and
cartridge
filter
systems
and
membrane
systems.
A
minimum
housing
area
of
50
ft2
was
assumed.
Housing
costs
were
generated
by
multiplying
the
footprint
area
by
an
average
housing
cost
of
$
48.95
per
square
foot
(
factory
building
in
RS
Means).

4.4.6.2
Summary
of
Bag
and
Cartridge
Filter
O&
M
Cost
Assumptions
O&
M
costs
for
bag
and
cartridge
filters
were
estimated
using
vendor
data
and
cost
estimating
guides.
Line
item
summaries
of
O&
M
costs
are
presented
in
Exhibits
4.32
and
4.33.
This
section
discusses
the
assumption
used
to
estimate
the
costs
presented
in
the
tables.

Bag
and
Cartridge
Replacement
The
average
cost
of
a
single
bag
or
cartridge,
as
well
as
the
average
number
of
bags
or
cartridges,
was
determined
based
on
vendor
estimates.
Cartridges
are
typically
more
durable
than
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
68
bags
and
require
less
frequent
replacement.
For
the
purposes
of
this
document,
it
was
assumed
that
cartridges
would
be
replaced
every
six
months
and
that
bags
would
be
replaced
every
three
months.

Power
Power
requirements
were
based
solely
on
the
additional
power
required
for
the
interstage
pumping.
Costs
were
estimated
based
on
pump
horsepower
ratings
(
see
Exhibit
4.31)
and
a
unit
cost
of
$
0.076
per
kWh.
A
linear
regression
was
completed
to
develop
the
following
equation
and
estimate
line
item
costs:

Power
($/
yr)
=
(­
286.6
×
Average
Flow2)
+
(
545.48
×
Average
Flow)
+
7.4011
Labor
Labor
requirements
are
considered
a
function
of
the
durability
of
the
bag
or
cartridge
filter
and
the
size
of
the
system.
For
systems
less
than
2
mgd,
one
hour
of
labor
per
month
plus
15
minutes
per
bag
or
cartridge
per
replacement
was
assumed.
For
systems
2
mgd
and
larger,
one
hour
of
labor
per
week
plus
15
minutes
per
bag
or
cartridge
per
replacement
was
assumed.
A
technical
labor
rate
of
$
24.96
was
applied
to
these
estimates
to
produce
labor
costs.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
69
Design
Flow
0.007
0.022
0.037
0.091
0.18
0.27
0.36
0.68
1
1.2
2
Average
Flow
0.0015
0.0054
0.0095
0.025
0.054
0.084
0.11
0.23
0.35
0.41
0.77
Unit
Capital
Cost
Summary
Total
Unit
Capital
Cost
$
10,280
$
10,421
$
12,828
$
13,320
$
19,487
$
23,423
$
28,771
$
42,479
$
65,654
$
75,011
$
136,788
Indirect
Capital
Costs
$
5,448
$
5,448
$
5,448
$
5,448
$
7,406
$
9,608
$
11,811
$
19,643
$
27,475
$
32,370
$
51,950
Operator
Training
$
500
$
500
$
500
$
500
$
500
$
500
$
500
$
500
$
500
$
500
$
500
Housing
$
2,448
$
2,448
$
2,448
$
2,448
$
4,406
$
6,608
$
8,811
$
16,643
$
24,475
$
29,370
$
48,950
Permitting
$
2,500
$
2,500
$
2,500
$
2,500
$
2,500
$
2,500
$
2,500
$
2,500
$
2,500
$
2,500
$
2,500
Capital
Cost
Multiplier
$
4,833
$
4,974
$
7,381
$
7,873
$
12,082
$
13,815
$
16,960
$
22,836
$
38,179
$
42,641
$
84,838
Subtotal
Process
Cost
$
4,027
$
4,145
$
6,151
$
6,561
$
10,068
$
11,512
$
14,133
$
19,030
$
31,816
$
35,535
$
50,801
Pipes
and
Valves
$
969
$
969
$
969
$
969
$
969
$
969
$
969
$
969
$
1,938
$
1,938
$
2,907
I&
C
$
969
$
969
$
969
$
969
$
969
$
969
$
969
$
969
$
1,938
$
1,938
$
2,907
Pumping
$
200
$
317
$
433
$
843
$
1,492
$
2,113
$
2,698
$
4,494
$
5,845
$
6,463
$
7,193
Bag
Filters
$
48
$
48
$
97
$
97
$
145
$
194
$
291
$
485
$
775
$
969
$
1,454
Filter
Housing
$
1,841
$
1,841
$
3,682
$
3,682
$
6,493
$
7,268
$
9,206
$
12,113
$
21,319
$
24,226
$
36,340
Annual
O&
M
Summary
Total
Annual
O&
M
Cost
$
527
$
529
$
750
$
758
$
992
$
1,226
$
1,676
$
2,605
$
3,963
$
4,858
$
8,119
Bag
Replacement
$
194
$
194
$
388
$
388
$
581
$
775
$
1,163
$
1,938
$
3,101
$
3,876
$
5,814
Electricity
$
8
$
10
$
13
$
21
$
36
$
51
$
64
$
118
$
163
$
183
$
257
Labor
$
324
$
324
$
349
$
349
$
374
$
399
$
449
$
549
$
699
$
799
$
2,047
Exhibit
4.32:
Bag
Filter
Cost
Summary
Source:
Section
4.4.6
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
70
Design
Flow
0.007
0.022
0.037
0.091
0.18
0.27
0.36
0.68
1
1.2
2
Average
Flow
0.0015
0.0054
0.0095
0.025
0.054
0.084
0.11
0.23
0.35
0.41
0.77
Unit
Capital
Cost
Summary
Total
Unit
Capital
Cost
$
10,465
$
10,606
$
13,197
$
17,256
$
24,024
$
31,480
$
43,699
$
73,535
$
111,151
$
136,393
$
265,091
Indirect
Capital
Cost
$
5,448
$
5,448
$
5,448
$
5,448
$
7,406
$
9,608
$
11,811
$
19,643
$
27,475
$
32,370
$
51,950
Operator
Training
$
500
$
500
$
500
$
500
$
500
$
500
$
500
$
500
$
500
$
500
$
500
Housing
$
2,448
$
2,448
$
2,448
$
2,448
$
4,406
$
6,608
$
8,811
$
16,643
$
24,475
$
29,370
$
48,950
Permitting
$
2,500
$
2,500
$
2,500
$
2,500
$
2,500
$
2,500
$
2,500
$
2,500
$
2,500
$
2,500
$
2,500
Capital
Cost
Multiplier
$
5,017
$
5,158
$
7,750
$
11,808
$
16,619
$
21,871
$
31,888
$
53,892
$
83,676
$
104,023
$
213,141
Subtotal
Process
Cost
$
4,181
$
4,298
$
6,458
$
9,840
$
13,849
$
18,226
$
26,573
$
44,910
$
69,730
$
86,686
$
127,629
Pipes
and
Valves
$
969
$
969
$
969
$
969
$
969
$
969
$
969
$
969
$
1,938
$
1,938
$
2,907
I&
C
$
969
$
969
$
969
$
969
$
969
$
969
$
969
$
969
$
1,938
$
1,938
$
2,907
Pumping
$
200
$
317
$
433
$
843
$
1,492
$
2,113
$
2,698
$
4,494
$
5,845
$
6,463
$
7,193
Cartridge
Filters
$
202
$
202
$
404
$
566
$
1,213
$
2,062
$
2,556
$
4,561
$
6,711
$
8,513
$
12,870
Filter
Housing
$
1,841
$
1,841
$
3,682
$
6,493
$
9,206
$
12,113
$
19,381
$
33,917
$
53,298
$
67,834
$
101,751
Annual
O&
M
Summary
Total
Annual
O&
M
Cost
$
725
$
727
$
1,146
$
1,490
$
2,836
$
4,600
$
5,625
$
9,826
$
14,321
$
18,082
$
28,157
Cartridge
Replacement
$
404
$
404
$
809
$
1,132
$
2,426
$
4,125
$
5,112
$
9,121
$
13,421
$
17,025
$
25,741
Electricity
$
8
$
10
$
13
$
21
$
36
$
51
$
64
$
118
$
163
$
183
$
257
Labor
$
312
$
312
$
324
$
337
$
374
$
424
$
449
$
587
$
736
$
874
$
2,159
Exhibit
4.33
Cartridge
Filter
Cost
Summary
Source:
Section
4.4.6
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
71
4.4.7
Bank
Filtration
Because
bank
filtration
has
not
been
a
widely
used
technology,
little
cost
data
are
available.
In
2000,
design
experts
from
the
Technical
Work
Group
(
TWG)
were
asked
to
estimate
a
cost
for
three
plant
sizes:
0.6,
6.5,
and
55
mgd.
Costs
for
other
plant
sizes
were
derived
from
these
estimates.
Plants
less
than
0.6
mgd
in
design
flow
were
assumed
to
incur
the
same
costs
as
a
0.6
mgd
plant.
Costs
for
plants
with
greater
than
0.6
mgd
were
calculated
assuming
a
linear
cost
versus
design
flow
function.
The
costs
provided
by
the
TWG
are
given
in
Exhibit
4.34.

Exhibit
4.34:
Bank
Filtration
Cost
Estimates
for
Three
System
Sizes
Design
Flow
(
mgd)
Capital
Cost
($)
O
&
M
Cost
($)

0.6
150,000
0
6.5
1,625,000
0
55
13,750,000
0
Source:
TWG
4.4.8
Second
Stage
Filtration
Chapter
3
provides
design
criteria
for
systems
to
receive
0.5
log
credit
for
Cryptosporidium
inactivation
using
second
stage
filtration.
Because
second
stage
filtration
has
not
been
a
widely
used
technology,
little
cost
data
are
available.
Design
experts
from
the
TWG
were
asked
to
estimate
a
cost
for
three
bank
filtration
plant
sizes
that
meet
the
criteria
in
Chapter
3:
0.6,
6.5,
and
55
mgd.
Costs
for
other
size
plants
were
derived
from
these
estimates.
Plants
less
than
0.6
mgd
in
design
flow
were
assumed
to
incur
the
same
costs
as
a
0.6
mgd
plant.
Costs
for
plants
with
greater
than
0.6
mgd
were
calculated
by
assuming
a
linear
cost
versus
design
flow
function.
The
costs
provided
by
the
TWG
are
given
in
Exhibit
4.35.

Exhibit
4.35:
Second
Stage
Filtration
Cost
Estimates
for
Three
System
Sizes
Design
Flow
(
mgd)
Capital
Cost
($)
O
&
M
Cost
($)

0.6
1,106,000
62,300
6.5
5,550,000
148,500
55
20,600,000
393,000
Source:
TWG
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
72
4.4.9
Pre­
Sedimentation
Chapter
3
provides
design
criteria
for
systems
to
receive
0.5
log
credit
for
Cryptosporidium
inactivation
using
pre­
sedimentation
basins.
Because
pre­
sedimentation
basins
have
not
been
a
widely
used
technology,
little
cost
data
are
available
for
this
technology.
Design
experts
from
the
TWG
were
asked
to
estimate
a
cost
for
three
plant
sizes,
which
met
the
design
criteria
in
Chapter
3:
0.6,
6.5,
and
55
mgd.
Costs
for
other
plant
sizes
were
derived
from
these
estimates.
Plants
less
than
0.6
mgd
in
design
flow
were
assumed
to
incur
the
same
costs
as
a
0.6
mgd
plant.
Costs
for
plants
with
greater
than
0.6
mgd
were
calculated
by
assuming
a
linear
cost
versus
design
flow
function.
The
costs
provided
by
the
TWG
are
given
in
Exhibit
4.36.

Exhibit
4.36:
Pre­
Sedimentation
Cost
Estimates
for
Three
System
Sizes
Design
Flow
(
mgd)
Capital
Cost
($)
O
&
M
Cost
($)

0.6
1,200,000
37,000
6.5
3,700,000
119,000
55
25,500,000
560,000
Source:
TWG
4.4.10
Watershed
Control
Chapter
3
provides
criteria
for
systems
to
receive
Cryptosporidium
inactivation
credit
for
watershed
control.
Because
each
watershed
control
program
will
be
site­
specific,
it
is
difficult
to
estimate
costs
for
such
programs.
However,
the
TWG
provided
EPA
with
rough
estimates
of
capital
and
O&
M
costs,
based
on
flow
for
a
program
that
meets
the
criteria
outlined
in
Chapter
3.
Capital
costs
are
assumed
to
include
development
of
an
oocyst
loading
model,
as
well
as
associated
validation
monitoring.
These
capital
costs
are
$
250,000
for
small
systems,
$
500,000
for
medium
systems,
and
$
1,000,000
for
large
systems.
O&
M
costs
are
divided
into
three
categories:
agreements
and
legal
mechanisms
to
mitigate
sources,
staff
and
resources
to
mitigate
sources
in
the
watershed,
and
public
health
surveillance
for
Cryptosporidium.
O&
M
costs
for
these
categories
and
for
three
system
sizes
are
shown
in
Exhibit
4.37.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
73
Exhibit
4.37:
Watershed
Cost
Categories
for
Three
System
Sizes
Watershed
Program
Component
O&
M
Cost
($)

Small
(
0.6
mgd)
Medium
(
6.5
mgd)
Large
(
55
mgd)

Agreements
and
Legal
Mechanisms
to
Mitigate
Sources
150,000
500,000
1,000,000
Demonstrated
Staff/
Resource
Commitment
to
Mitigate
Sources
100,000
250,000
1,000,000
Public
Health
Surveillance
for
Cryptosporidium
100,000
250,000
500,000
Source:
TWG
4.4.11
Combined
Filter
Performance
Combined
filter
performance
is
not
a
single
technology,
but
a
variety
of
actions
that
a
system
can
take
to
achieve
0.15
NTU
combined
filter
effluent
concentration
95
percent
of
the
time.
Chapter
3
provides
a
list
of
actions
or
steps
that
a
plant
could
take
to
reduce
effluent
turbidity.
The
actions
are:

°
Chemical
Addition
 
Installing
backwash
polymer
feed
capability
 
Coagulant
improvement
 
Adding
primary
coagulant
feed
points
°
Filter
Improvements
 
Filter
media
addition
 
Post
backwash
filter­
to­
waste
 
Filter
rate­
of­
flow
controller
°
Process
Management
Changes
 
Plant
staffing
increase
 
Staff
qualifications
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
74
°
Laboratory
Modifications
 
Turbidimeter
purchase
 
Jar
test
apparatus
purchase
 
Purchase
a
particle
counter
or
other
alternative
process
control
testing
equipment
°
Process
Control
Testing
Modification
 
Staff
Training
Each
action
was
costed
individually.
Then
the
proportion
of
plants
selecting
each
action
was
estimated.
Percentages
were
multiplied
by
the
individual
unit
costs
to
arrive
at
an
average
unit
cost.

Similar
assumptions
were
used
for
all
of
the
steps
involving
filtration.
The
assumptions
regarding
filter
size
and
flow
were
the
same
for
filter
media
addition,
filter­
to­
waste,
and
filter
rate­
offlow
controller
replacement.
Exhibit
4.38
summarizes
the
design
assumptions
used
in
estimating
capital
and
O&
M
costs
for
filtration
improvements.
A
conservative
filter
design
loading
rate
(
2.5
gpm/
ft2)
was
used
to
estimate
the
number
of
filters.
The
number
of
filters
was
based
on
a
maximum
filter
area
 
125
ft2,
250
ft2,
700
ft2,
or
1,000
ft2
 
determined
by
system
size.
The
total
number
of
filters
was
based
on
the
number
of
filters
required
to
produce
the
design
flow
at
the
design
loading
rate
plus
one
(
n+
1).
Filter
piping
diameters
were
determined
using
the
criteria
below
(
Water
Treatment
Plant
Design,
AWWA,
1969).

°
Filter
effluent
piping
velocity
=
3­
6
feet
per
second
(
fps)

°
Filter
to
waste
(
FTW)
piping
velocity
=
6­
12
fps
°
Drain
piping
velocity
=
3­
8
fps
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
75
Exhibit
4.38:
Summary
of
Filtration
Improvement
Design
Assumptions
Population
500
­
1,000
1,001
­
3,300
3,301
­
10,000
10,001­
50,000
50,001­
100,000
100,001­
1,000,000
>
1,000,000
Avg.
Flow
(
mgd)
0.093
0.250
0.626
2.758
5.082
23.671
109.707
Design
Flow
(
mgd)
0.245
0.633
1.511
6.277
11.040
48.429
205.503
Design
Filter
Loading
Rate
(
gpm/
sf)
2.5
2.5
2.5
2.5
2.5
2.5
2.5
Total
Filter
Area
(
sf)
68
176
420
1744
3067
13453
57084
Max
filter
area
(
sf)
125
125
250
700
700
700
1000
Number
of
Filters
2
3
3
4
6
21
59
Pipe
Sizing
Loading
Rate
(
gpm/
sf)
5
5
5
5
5
5
5
Flow
per
Filter
(
gpm)
340
440
1049
2906
3067
3363
4921
Effluent
Piping
Diameter
(
inches)
6
6
10
16
16
20
20
Filter
Effluent
Pipe
Velocity
(
fps)
3.9
5.0
4.3
4.6
4.9
3.4
5.0
FTW
Diameter
(
in)
4
6
8
12
12
14
16
FTW
Pipe
Velocity
(
fps)
8.7
5.0
6.7
8.2
8.7
7.0
7.9
Backwash
Rate
(
gpm/
sf)
20
20
20
20
20
20
20
Backwash
Flow
(
gpm)
1,361
1,758
4,197
11,624
12,267
13,453
19,684
Drain
Diameter
(
inches)
10
12
16
30
36
36
36
Drain
Pipe
Velocity
(
fps)
5.6
5.0
6.7
5.3
3.9
4.2
6.2
Source:
Section
4.4.11
Because
of
the
operator
attention
required
to
produce
such
low
turbidity
water
and
because
few
very
small
plants
are
conventional,
it
was
assumed
that
systems
serving
fewer
than
500
people
would
not
use
this
technology.
Also
construction,
engineering,
and
indirect
costs,
such
as
housing
or
permitting,
are
not
typically
included
in
the
cost
estimates.
This
is
because
most
of
these
actions
are
either
operational
changes
or
involve
very
little
capital
modifications.
Therefore,
costs
for
items
such
as
engineering
and
sitework
are
not
appropriate.

The
assumptions
behind
each
filter
improvement
action
are
given
in
section
4.4.11.1
to
4.4.11.11.
Unit
capital
and
O&
M
costs
for
each
action
are
summarized
in
Exhibits
4.40
and
4.41.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
76
4.4.11.1
Installing
Backwash
Polymer
Feed
Capital
costs
were
based
on
feeding
a
0.5
ppm
dose
of
polymer
from
a
0.25
percent,
by
weight,
solution.
The
backwash
duration
was
assumed
to
be
15
minutes
per
filter
at
a
backwash
rate
of
20
gpm/
ft2,
with
an
average
filter
run
of
three
days.
Conceptual
design
assumed
a
dry
polymer
feed
system
that
can
be
loaded
with
a
seven­
day
polymer
supply.
Extra
storage
capacity
for
dry
polymer
bags
was
assumed
within
the
plant.
Equipment
includes
mixing
tank,
solution
tank,
secondary
dilution
mixer,
and
metering
pumps.

Capital
costs
include
equipment,
installation
(
25
percent
of
equipment),
electrical
(
10
percent
of
equipment),
instrumentation
and
control
(
10
percent
of
equipment),
contingencies
(
30
percent
of
equipment,
installation,
electrical,
and
instrumentation
and
control),
contractor
overhead
and
profit
(
15
percent
of
equipment,
installation,
electrical,
and
instrumentation
and
control),
and
engineering
(
20
percent
of
equipment,
installation,
electrical,
and
instrumentation
and
control).

O&
M
costs
for
the
backwash
water
polymer
feed
system
include
polymer
cost
($
2.25
per
pound),
additional
maintenance
labor,
and
parts
and
materials
(
10
percent
of
equipment
cost
per
year).
A
labor
rate
of
$
24.96/
hr
was
used
for
all
labor
costs.

4.4.11.2
Installing
Additional
Coagulant
Feed
Points
Capital
costs
were
based
on
a
5
ppm
dose
of
primary
coagulant.
The
primary
coagulant
was
assumed
to
be
ferric
chloride,
ferric
sulfate,
or
alum.
Thirty
days
of
bulk
storage
were
assumed
for
ferric
chloride
or
ferric
sulfate
(
equivalent
to
approximately
15
days
of
storage
for
alum).
Equipment
includes
bulk
storage
tanks,
day
tanks,
metering
pumps,
pipes,
and
valves.

Capital
costs
include
equipment,
installation
(
25
percent
of
equipment),
electrical
(
10
percent
of
equipment),
instrumentation
and
control
(
10
percent
of
equipment),
contingencies
(
30
percent
of
equipment,
installation,
electrical,
and
instrumentation
and
control),
contractor
overhead
and
profit
(
15
percent
of
equipment,
installation,
electrical,
and
instrumentation
and
control),
and
engineering
(
20
percent
of
equipment,
installation,
electrical,
and
instrumentation
and
control).

O&
M
costs
for
expansion
of
the
coagulant
feed
system
include
coagulant
cost
($
350
per
ton),
additional
maintenance
labor,
and
parts
and
materials
(
10
percent
of
equipment
cost
per
year).
A
labor
rate
of
$
24.96/
hr
was
used
for
all
labor
costs.

4.4.11.3
Filter
Media
Addition
Individual
filter
area
and
number
of
filters
were
based
on
a
design
filter
loading
rate
of
2.5
gpm/
sf
as
listed
in
Exhibit
4.38.
It
was
assumed
that
only
anthracite
media
needs
to
be
replaced
(
i.
e.,
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
77
no
sand
media
losses
in
dual­
media
filters)
and
that
only
anthracite
media
is
added
to
increase
the
total
media
depth.
Topping
off
existing
media
was
assumed
to
require
2
inches
to
6
inches
of
anthracite
and
average
4
inches
of
anthracite
per
filter.
It
was
also
assumed
that
an
additional
6
inches
of
anthracite
media
is
added
to
each
filter
to
increase
the
total
media
depth,
giving
a
total
required
depth
of
10
inches.

Capital
costs
were
based
on
a
total
of
10
inches
additional
anthracite
media.
Costs
include
anthracite
media,
transportation
($
2/
mile
 
assumed
1,000
miles
 
plus
$
0.50/
lb),
installation
(
25
percent
of
media
cost),
contingencies
(
30
percent
of
media,
transportation,
and
installation),
contractor
overhead
and
profit
(
15
percent
of
media,
transportation,
and
installation),
and
engineering
(
20
percent
of
media,
transportation,
and
installation).
O&
M
costs
for
this
task
were
assumed
to
be
zero.

4.4.11.4
Filter
to
Waste
The
number
of
filters
was
based
on
design
filter
loading
rate
of
2.5
gpm/
ft2,
and
pipe
sizing
was
based
on
a
filter
loading
rate
of
5
gpm/
ft2,
as
listed
in
Exhibit
4.38.
Filter
effluent
piping,
filter­
to­
waste
piping,
and
drain
piping
sizes
are
also
listed
in
Exhibit
4.38.
Installing
filter­
to­
waste
capability
requires
modification
of
existing
filter
effluent
piping
and
connection
of
the
new
filter­
to­
waste
piping
to
the
filter
drain
piping.
The
extent
of
modifications
required
to
complete
these
modifications
can
vary
significantly
depending
on
plant
size
and
existing
piping
configuration.
The
cost
estimates
presented
were
based
on
the
following
assumptions:

°
Cutting
existing
pipe
°
Replacing
10
feet
of
filter
effluent
pipe
per
filter
°
Replacing
two
filter
effluent
valves
(
control
valve
and
isolation
valve)
per
filter
°
Installing
one
tee
in
filter
effluent
piping
for
FTW
piping
per
filter
°
Installing
one
filter­
to­
waste
isolation
valve
per
filter
°
Installing
25
feet
of
filter­
to­
waste
piping
and
four
90
degree
elbows
per
filter
°
Connecting
FTW,
including
conical
reducers
and
tees,
into
existing
drain
piping
Capital
costs
include
equipment,
installation
(
25
percent
of
equipment),
electrical
(
10
percent
of
equipment),
instrumentation
and
control
(
10
percent
of
equipment),
contingencies
(
30
percent
of
equipment,
installation,
electrical,
and
instrumentation
and
control),
contractor
overhead
and
profit
(
15
percent
of
equipment,
installation,
electrical,
and
instrumentation
and
control),
and
engineering
(
20
percent
of
equipment,
installation,
electrical,
and
instrumentation
and
control).
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
78
O&
M
costs
for
addition
of
filter­
to­
waste
capabilities
include
additional
labor
associated
with
longer
backwash/
filter­
to­
waste/
return­
to­
service
duration
(
15
minutes
per
filter
per
backwash),
additional
maintenance
labor
(
1
hour
per
filter
per
month),
and
parts
and
materials
(
10
percent
of
equipment
cost
per
year).
A
labor
rate
of
$
24.96/
hr
was
used
for
all
labor
costs.
Filter
run
time
between
backwashes
was
assumed
to
be
72
hours.

4.4.11.5
Filter
Rate­
of­
Flow
Controller
Replacement
Number
of
filters
was
based
on
a
design
filter
loading
rate
of
2.5
gpm/
ft2,
and
pipe
sizing
was
based
on
a
filter
loading
rate
of
5
gpm/
ft2,
as
listed
in
Exhibit
4.38.
Filter
effluent
piping
sizes
are
also
listed
in
Exhibit
4.38.
Installing
or
replacing
the
filter
rate­
of­
flow
controller
requires
replacement
of
existing
filter
effluent
piping
and
valves.
The
extent
of
modifications
required
to
complete
these
modifications
can
vary
significantly
depending
on
plant
size
and
existing
piping
configuration.
The
cost
estimates
presented
were
based
on
the
following
assumptions:

°
Cutting
existing
pipe
°
Replacing
10
feet
of
filter
effluent
pipe
per
filter
°
Replacing
two
filter
effluent
valves
(
control
valve
and
isolation
valve)
per
filter
°
Installing/
Replacing
a
venturi
meter
Capital
costs
include
equipment,
installation
(
25
percent
of
equipment),
electrical
(
10
percent
of
equipment),
instrumentation
and
control
(
10
percent
of
equipment),
contingencies
(
30
percent
of
equipment,
installation,
electrical,
and
instrumentation
and
control),
contractor
overhead
and
profit
(
15
percent
of
equipment,
installation,
electrical,
and
instrumentation
and
control),
and
engineering
(
20
percent
of
equipment,
installation,
electrical,
and
instrumentation
and
control).

O&
M
costs
for
addition
or
replacement
of
filter
rate­
of­
flow
controllers
include
additional
maintenance
labor
(
1
hour
per
filter
per
month),
electricity
(
based
on
valve
actuator
horsepower
and
a
motor
efficiency
of
70
percent),
and
parts
and
materials
(
10
percent
of
equipment
cost
per
year).
Exhibit
4.39
shows
the
assumptions
for
valve
actuator
horsepower.
Horsepowers
are
based
on
experience
with
similar
systems
and
vender
quotes.
A
labor
rate
of
$
24.96/
hr
was
used
for
all
labor
costs.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
79
Exhibit
4.39:
Valve
Actuator
Horsepower
Assumptions
Valve
Diameter
(
in)
Actuator
Horsepower
(
Hp)

<
8
1/
50
<
14
1/
6
<
24
1/
4
>
24
1
4.4.11.6
Increase
Plant
Staffing
A
capital
cost
of
$
6,000
per
new
staff
or
fraction
thereof
for
office
and
field
fixtures,
computer
hardware,
and
training
was
assumed.
The
O&
M
costs
were
developed
assuming
labor
increases
between
10
and
120
hours
per
week,
depending
on
system
size.
Systems
serving
3,300
or
fewer
people
were
assumed
to
increase
labor
by
ten
hours
per
week
(
0.25
operator).
Systems
serving
between
3,301
and
50,000
people
were
assumed
to
hire
one
half­
time
operator.
Systems
serving
between
50,001
and
100,000
people
were
assumed
to
hire
one
additional
operator.
Systems
serving
between
100,001
and
1,
000,000
people
were
assumed
to
hire
two
additional
operators.
Systems
serving
1,000,000
or
more
people
were
assumed
to
hire
three
operators.
Costs
were
based
on
an
hourly
labor
rate
of
$
24.96
for
trained
operators.

4.4.11.7
Update
Plant
Staff
Qualifications
No
capital
costs
were
associated
with
this
estimate.
The
O&
M
costs
were
calculated
including
an
annual
allowance
for
training
staff
members.
The
best
means
of
continuing
the
education
of
staff
is
through
local
or
state
operator
certification
training.
Using
current
AWWA
prices
(
March
2003),
class
fees
per
operator
were
assumed
to
be
$
260
for
systems
serving
10,000
people
or
fewer
and
$
400
for
systems
serving
more
than
10,000
people.
Systems
serving
10,000
people
or
fewer
were
assumed
to
send
one
operator.
Systems
serving
between
10,001
and
100,000
people
were
assumed
to
send
two
operators.
Systems
serving
between
100,001
and
1,000,000
people
were
assumed
to
send
four
operators.
It
was
assumed
that
systems
serving
more
than
1,000,000
people
would
send
six
operators
to
the
training
course.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
80
4.4.11.8
Purchase
Turbidimeter
This
step
involves
replacing
obsolete
bench­
top
or
on­
line
turbidimeters
with
new
on­
line
units
with
electronic
data
acquisition
interface.
Based
on
vendor
quotes,
the
cost
for
a
conventional
turbidimeter,
including
shipping
and
installation,
was
estimated
to
be
$
3,242,
and
the
cost
of
a
laser
turbidimeter,
including
shipping
and
installation,
was
estimated
to
be
$
5,449.

For
systems
serving
more
than
10,000
people,
it
was
assumed
that
laser
turbidity
meters
will
be
purchased.
For
systems
serving
10,000
or
fewer
people
it
was
assumed
that
standard
on­
line
turbidimeters
will
be
purchased.
It
was
assumed
that
systems
serving
more
than
1,000,000
people
would
purchase
six
additional
laser
turbidimeters.
Systems
serving
between
100,001
and
1,000,000
people
were
assumed
to
purchase
four
additional
laser
instruments.
Systems
serving
between
50,001and100,000
people
were
assumed
to
purchase
two
additional
laser
instruments.
Systems
serving
between
10,001
and
50,000
people
were
assumed
to
purchase
one
additional
instrument
(
laser).
Systems
serving
10,000
people
or
fewer
were
assumed
to
purchase
one
additional
standard
on­
line
instrument.

The
O&
M
costs
were
calculated
considering
annual
maintenance
material
and
labor
required
for
general
maintenance
and
monthly
calibration
of
the
equipment.
For
each
additional
instrument,
twenty
hours
per
year
were
assumed
to
be
required
for
labor
at
the
hourly
rate
of
$
24.96.

4.4.11.9
Purchase
Jar
Test
Apparatus
Based
on
vendor
quotes
the
cost
of
a
six­
paddled
stirrer
with
two
liter
jars,
including
shipping,
was
estimated
to
be
$
2,722.
Systems
serving
100,000
people
or
fewer
were
assumed
to
purchase
one
apparatus.
Systems
serving
between
100,001
and
1,000,000
people
were
assumed
to
purchase
two
apparatuses.
It
was
assumed
that
systems
serving
more
than
1,000,000
people
would
purchase
three
apparatuses.

More
frequent
jar
testing
may
be
required
to
optimize
chemical
addition
during
coagulation.
It
has
been
assumed
that
seven
hours
per
week
will
be
required
to
operate
each
jar
testing
apparatus.

4.4.11.10
Purchase
Particle
Counters
Based
on
vendor
quotes,
the
cost
of
a
particle
counter
with
interface
for
data
acquisition
system
was
estimated
to
be
$
6,024.
It
was
assumed
that
only
systems
serving
more
than
1,000
people
would
purchase
the
instrument.
Systems
serving
between
1,001
and
100,000
people
were
assumed
to
purchase
one
instrument.
Systems
serving
between
100,001
and
1,000,000
people
were
assumed
to
purchase
two
particle
counters.
Systems
serving
more
than
1,000,000
people
were
assumed
to
purchase
three
particle
counters.
It
was
assumed
that
20
hours
per
unit
would
be
required
for
installation
and
initial
calibration
of
each
unit.
It
was
assumed
that
40
hours
of
labor
per
year
would
be
required
for
the
calibration
and
maintenance
of
each
instrument.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
81
System
Population
Size
Categories
501­
1,000
1,001­
3,300
3,301­
10,000
10,001
­
50,000
50,001
­
100,000
100,001
­
1,000,000
>
1,000,000
Chemical
Addition
Install
backwash
water
polymer
feed
capability
$
113,000
$
113,000
$
118,300
$
126,200
$
126,200
$
210,300
$
323,300
Coagulant
Improvements
Primary
coagulant
feed
points,
control,
measurement
$
36,300
$
37,400
$
57,500
$
116,000
$
128,400
$
207,900
$
703,300
Filtration
Improvements
Filter
media
additions
(
10"
typical)
$
5,900
$
9,500
$
19,800
$
67,800
$
106,100
$
401,600
$
1,644,900
Post
backwash
filter­
to­
waste
$
18,900
$
38,100
$
70,700
$
243,900
$
434,600
$
1,906,300
$
5,436,900
Filter
rate­
of­
flow
controller
replacement
$
21,360
$
38,079
$
94,418
$
233,728
$
479,684
$
2,749,255
$
9,801,092
Process
Managament
Changes
Plant
staffing
increase
$
1,500
$
1,500
$
3,000
$
3,000
$
6,000
$
12,000
$
18,000
Staff
qualifications
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Laboratory
Modifications
Purchase
on­
line
turbidimeter
with
data
acquisition
interface
$
3,243
$
3,243
$
3,243
$
5,449
$
21,796
$
87,184
$
196,164
Jar
test
apparatus
purchase
$
2,722
$
2,722
$
2,722
$
2,722
$
2,722
$
5,444
$
8,166
Alternative
process
control
testing
equipment,
particle
counter
$
0
$
6,523
$
6,523
$
6,523
$
6,523
$
13,046
$
19,570
Process
Control
Modifications
Staff
training
(
consultant
as
trainer)
$
0
$
0
$
0
$
0
$
0
$
0
$
0
4.4.11.11
Staff
Training
No
capital
costs
were
associated
with
this
estimate.
The
costs
associated
with
this
estimate
were
assumed
to
be
an
annual
O&
M
commitment
for
training
all
staff
members
and
were
based
on
an
average
consultant
hourly
wage
of
$
100/
hour.
The
O&
M
costs
were
developed
assuming
between
14
and
140
hours
of
consultant
time,
depending
on
the
size
of
the
system.
The
hours
budgeted
for
consultants
include
time
spent
on
site
conducting
training
and
time
for
customizing
the
training.

Exhibit
4.40:
Capital
Unit
Costs
for
Combined
Filter
Performance
Components
Source:
Section
4.4.11
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
82
System
Population
Size
Categories
501­
1,000
1,001­
3,300
3,301­
10,000
10,001
­
50,000
50,001
­
100,000
100,001
­
1,000,000
>
1,000,000
Chemical
Addition
Install
backwash
water
polymer
feed
capability
$
6,000
$
6,100
$
6,700
$
8,000
$
8,300
$
16,300
$
36,700
Coagulant
Improvements
Primary
coagulant
feed
points,
control,
measurement
$
2,000
$
2,300
$
3,200
$
8,800
$
14,100
$
54,000
$
199,800
Filtration
Improvements
Filter
media
additions
(
10"
typical)
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Post
backwash
filter­
to­
waste
$
2,300
$
3,600
$
3,900
$
6,600
$
10,500
$
40,700
$
116,200
Filter
rate­
of­
flow
controller
replacement
$
2,500
$
3,800
$
5,400
$
8,700
$
13,100
$
47,800
$
134,300
Process
Managament
Changes
Plant
staffing­
increase
$
12,979
$
12,979
$
25,958
$
25,958
$
51,917
$
103,834
$
155,750
Staff
qualifications
$
460
$
460
$
659
$
1,199
$
1,599
$
3,197
$
4,796
Laboratory
Modifications
Purchase
on­
line
turbidimeter
with
data
acquisition
interface
$
684
$
684
$
684
$
724
$
1,223
$
2,447
$
3,445
Jar
test
apparatus
purchase
$
9,085
$
9,085
$
9,085
$
9,085
$
9,085
$
18,171
$
27,256
Alternative
process
control
testing
equipment­
$
0
$
1,239
$
1,239
$
1,239
$
1,239
$
2,238
$
3,236
Particle
counter
Process
Control
Modifications
Staff
training
(
consultant
as
trainer)
$
1,400
$
1,600
$
2,800
$
5,000
$
7,000
$
10,000
$
14,000
Exhibit
4.41:
O&
M
Unit
Costs
for
Combined
Filter
Performance
Components
Source:
Section
4.4.11
4.4.11.12
Average
Plant
Cost
Percentages
of
plants
using
each
of
the
filter
performance
options
described
in
4.4.11.1
through
4.4.11.11
were
determined
using
best
professional
judgement.
The
percentages
do
not
add
to
100
as
many
systems
will
have
to
use
more
than
one
of
the
steps
to
achieve
the
desired
reduction
in
CFE
turbidity.
Exhibit
4.42
shows
the
percentages
used.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
83
System
Population
Size
Categories
501­
1,000
1,001­
3,300
3,301­
10,000
10,001­
50,000
50,001­
100,000
100,001­
1,000,000
>
1,000,000
Chemical
Addition
Install
backwash
water
polymer
feed
capability
10%
10%
10%
10%
10%
10%
10%

Coagulant
Improvements
Primary
coagulant
feed
points,
control,
measurement
0%
5%
10%
10%
10%
10%
10%

Filtration
Improvements
Filter
media
additions
(
10"
typical)
5%
10%
15%
20%
20%
20%
20%
Post
backwash
filter­
to­
waste
5%
5%
5%
5%
5%
5%
5%
Filter
rate­
of­
flow
controller
replacement
15%
15%
15%
15%
15%
15%
15%

Process
Managament
Changes
Plant
staffing­
increase
100%
100%
100%
100%
100%
100%
100%
Staff
qualifications
100%
100%
100%
100%
100%
100%
100%

Laboratory
Modifications
Bench
top
turbidimeter
purchase­
replace
obsolete
units
10%
10%
10%
10%
10%
10%
10%
Jar
test
apparatus
purchase
10%
10%
10%
10%
10%
10%
10%
Alternative
process
control
testing
equipment,
particle
counter
10%
10%
10%
20%
20%
20%
20%

Process
Control
Modifications
Staff
training
(
consultant
as
trainer)
80%
80%
80%
80%
80%
80%
80%
Exhibit
4.42:
Percentages
of
Plants
Using
Each
Filter
Improvement
Option
Source:
Section
4.4.11
To
computer
an
average
capital
and
O&
M
cost
for
all
plants
using
the
combined
filter
performance
toolbox
option,
the
percentages
were
multiplied
by
the
capital
and
O&
M
costs
for
each
of
the
processes
from
Exhibits
4.40
and
4.41.
Exhibits
4.43
and
4.44
show
the
final
capital
and
O&
M
costs
used
for
plants
using
combined
filter
performance
to
achieve
LT2ESWTR
compliance.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
84
System
Population
Size
Categories
501­
1,000
1,001­
3,300
3,301­
10,000
10,001
­
50,000
50,001
­
100,000
100,001
­
1,000,000
>
1,000,000
Chemical
Addition
Install
backwash
water
polymer
feed
capability
$
11,300
$
11,300
$
11,830
$
12,620
$
12,620
$
21,030
$
32,330
Coagulant
Improvements
Primary
coagulant
feed
points,
control,
measurement
$
0
$
1,870
$
5,750
$
11,600
$
12,840
$
20,790
$
70,330
Filtration
Improvements
Filter
media
additions
(
10"
typical)
$
295
$
950
$
2,970
$
13,560
$
21,220
$
80,320
$
328,980
Post
backwash
filter­
to­
waste
$
945
$
1,905
$
3,535
$
12,195
$
21,730
$
95,315
$
271,845
Filter
rate­
of­
flow
controller
replacement
$
3,204
$
5,712
$
14,163
$
35,059
$
71,953
$
412,388
$
1,470,164
Process
Managament
Changes
Plant
staffing
increase
$
1,500
$
1,500
$
3,000
$
3,000
$
6,000
$
12,000
$
18,000
Staff
qualifications
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Laboratory
Modifications
Purchase
on­
line
turbidimeter
with
data
acquisition
interface
$
324
$
324
$
324
$
545
$
2,180
$
8,718
$
19,616
Jar
test
apparatus
purchase
$
272
$
272
$
272
$
272
$
272
$
544
$
817
Alternative
process
control
testing
equipment,
particle
counter
$
0
$
652
$
652
$
1,305
$
1,305
$
2,609
$
3,914
Process
Control
Modifications
Staff
training
(
consultant
as
trainer)
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Total
17,840
24,486
42,497
90,156
150,119
653,715
2,215,996
Exhibit
4.43:
Capital
Cost
Estimates
for
the
Combined
Filter
Performance
Source:
Capital
costs
from
Exhibit
4.40
multiplied
by
percentages
in
Exhibit
4.42.
"
Total"
represents
the
average
cost
per
plant.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
85
System
Population
Size
Categories
501­
1,000
1,001­
3,300
3,301­
10,000
10,001
­
50,000
50,001
­
100,000
100,001
­
1,000,000
>
1,000,000
Chemical
Addition
Install
backwash
water
polymer
feed
capability
$
600
$
610
$
670
$
800
$
830
$
1,630
$
3,670
Coagulant
Improvements
Primary
coagulant
feed
points,
control,
measurement
$
0
$
115
$
320
$
880
$
1,410
$
5,400
$
19,980
Filtration
Improvements
Filter
media
additions
(
10"
typical)
$
0
$
0
$
0
$
0
$
0
$
0
$
0
Post
backwash
filter­
to­
waste
$
115
$
180
$
195
$
330
$
525
$
2,035
$
5,810
Filter
rate­
of­
flow
controller
replacement
$
375
$
570
$
810
$
1,305
$
1,965
$
7,170
$
20,145
Process
Managament
Changes
Plant
staffing­
increase
$
12,979
$
12,979
$
25,958
$
25,958
$
51,917
$
103,834
$
155,750
Staff
qualifications
$
460
$
460
$
659
$
1,199
$
1,599
$
3,197
$
4,796
Laboratory
Modifications
Purchase
on­
line
turbidimeter
with
data
acquisition
interface
$
68
$
68
$
68
$
72
$
122
$
245
$
345
Jar
test
apparatus
purchase
$
909
$
909
$
909
$
909
$
909
$
1,817
$
2,726
Alternative
process
control
testing
equipment­
$
0
$
124
$
124
$
248
$
248
$
448
$
647
Particle
counter
Process
Control
Modifications
Staff
training
(
consultant
as
trainer)
$
1,120
$
1,280
$
2,240
$
4,000
$
5,600
$
8,000
$
11,200
Total
16,626
17,295
31,954
35,702
65,124
133,775
225,069
Exhibit
4.44:
O&
M
Costs
for
the
Combined
Filter
Performance
Source:
O&
M
costs
from
Exhibit
4.41
multiplied
by
the
percentages
in
Exhibit
4.42.
"
Total"
represents
the
average
O&
M
cost
per
plant.

4.5
DBP
Precursor
and
Microbial
Removal
Technologies
This
section
presents
capital
and
O&
M
estimates
for
new
or
enhanced
technologies
employed
for
the
removal
of
DBP
precursors.
It
should
be
noted
that
all
of
the
technologies
discussed
in
this
section
may
not
be
applicable
for
all
systems.

4.5.1
Granular
Activated
Carbon
Adsorption
Costs
for
GAC
adsorption
were
estimated
for
two
EBCTs:
10
minutes
and
20
minutes.
Installation
of
the
GAC
contactors
was
assumed
to
be
after
filtration.
The
number
of
contactors
(
n)
varies
by
system
size,
with
a
minimum
of
two
operating
contactors
to
take
advantage
of
blending.
Exhibit
4.45
presents
the
number
of
contactors
assumed
for
each
system
size
for
which
costs
are
presented.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
86
Exhibit
4.45:
GAC
Contactor
Assumptions
Design
Flow
(
mgd)
Number
of
Contactors
0.024
0.087
0.1
0.27
0.45
0.65
0.83
1
10
11
18
26
51
210
430
520
n
2
2
4
4
5
5
5
5
10
10
10
10
10
20
20
20
n+
1
3
3
5
5
6
6
6
6
11
11
11
11
11
21
21
21
Note:
n
=
number
of
operating
contactors
n+
1
=
number
of
contactors
including
redundant
contactors,
which
are
used
for
costing
Source:
Calculated
based
on
flow
and
reactor
size.

Costs
are
also
presented
for
a
range
of
reactivation
frequencies
(
90,
240,
and
360
days)
to
account
for
variability
in
source
water
quality.
For
an
EBCT
of
10
minutes,
costs
are
presented
for
reactivation
frequency
of
360
days.
For
an
EBCT
of
20
minutes,
costs
are
presented
for
reactivation
frequencies
of
90
and
240
days.
The
reactivation
frequency
is
a
function
of
the
number
of
contactors
and
system
size.
The
reactivation
frequency
identified
(
e.
g.,
90
days)
represents
the
reactivation
frequency
of
the
largest
system
for
which
costs
are
provided
(
430
mgd).
The
frequency
for
systems
with
fewer
than
20
contactors
(
i.
e.,
the
number
of
operating
contactors
assumed
for
the
largest
system)
is
actually
a
fraction
of
the
frequency
identified.
The
correlation
between
n
and
blended
run
time
is
based
upon
results
presented
in
Analysis
of
GAC
Effluent
Blending
During
the
ICR
Treatment
Studies
(
USEPA
1999a),
which
includes
an
analysis
of
the
incremental
increase
in
blended
run
time
attributable
to
the
addition
of
a
contactor
in
parallel.
The
true
reactivation
frequencies
for
each
system
size
are
presented
in
Exhibits
4.46
through
4.48.

4.5.1.1
Summary
of
GAC
Capital
Cost
Assumptions
Costs
were
generally
obtained
from
the
Water
model.
Some
cost
components
were
based
on
vendor
quotes;
these
were
discounted
to
year
2000
dollars
using
the
ENR
BCI.

Process
Costs
At
least
two
contactors
were
assumed
to
be
in
service
with
one
stand­
by.
Exhibit
4.45
summarizes
the
number
of
contactors
or
pressure
vessels
assumed
for
each
flow
category.
Systems
with
design
flows
of
less
than
1
mgd
were
assumed
to
use
package
plants.

GAC
Contactor,
Media,
and
Regeneration
Furnace
Costs
(
large
systems)

For
large
systems
(>
1
mgd
design
flow),
the
capital
costs
for
GAC
contactor,
initial
media,
and
regeneration
furnace
were
obtained
from
the
Water
model.
The
model
was
used
to
calculate
the
capital
costs,
based
on
design
flow,
average
operating
flow,
EBCT,
and
regeneration
frequency.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
87
Capital
costs
include
concrete
gravity
contactors
operated
at
a
loading
rate
5
gpm/
ft2,
troughs
and
pipes
for
carbon
removal
as
a
slurry,
initial
virgin
carbon.

Large
systems
regenerate
on­
site
utilizing
a
multiple­
hearth
furnace.
The
size
of
the
furnace
is
affected
by
the
carbon
usage
rate,
which
is
affected
by
the
reactivation
frequency.
A
loading
rate
of
50
lb/
ft2
per
day
was
assumed
for
all
systems.

For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
GAC
Contactor
and
Regeneration
Furnace
($)
=
194516
×
(
Design
Flow)
0.751
For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
GAC
Contactor
and
Regeneration
Furnace($)
=
298015
×
(
Design
Flow)
0.7876
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
GAC
Contactor
and
Regeneration
Furnace
($)
=
370226
×
(
Design
Flow)
0.7562
Package
GAC
System
Costs
(
Small
Systems)

For
small
systems
(
0.1­
1.0
mgd
design
flow),
the
capital
costs
for
package
units
were
estimated
using
the
Water
model.
Capital
costs
include
pressure
vessels,
factory­
assembled
contactors
mounted
on
steel
skid,
initial
charge
of
activated
carbon,
supply
and
backwash
pump,
valves,
piping,
and
pressure
gauges,
and
electrical
control
panels.

For
very
small
systems
(<
0.1
mgd
design
flow),
the
capital
costs
for
GAC
package
units
were
estimated
using
the
VSS
Model.
Capital
costs
include
GAC
pressure
contactor
vessels,
virgin
GAC,
pipes
and
valves,
and
instrumentation
and
controls.

Because
small
and
very
small
systems
operate
on
a
replacement
basis,
capital
costs
are
unaffected
by
reactivation
frequency
or
carbon
usage
rate.
As
a
result,
capital
costs
for
small
systems
vary
only
by
EBCT
and
design
flow.

For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
GAC
Package
Plant
($)
=
­
33425
×
(
Design
Flow)
2+
332500
×
(
Design
Flow)
+
17765
For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
GAC
Package
Plant
($)
=
­
129710
×
(
Design
Flow)
2+
640704
×
(
Design
Flow)
+
10721
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
GAC
Package
Plant
($)
=
­
129710
×
(
Design
Flow)
2+
640704
×
(
Design
Flow)
+
10721
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
88
Piping
and
Valves
Costs
For
large
systems,
the
capital
costs
for
pipes
and
valves
were
obtained
from
the
Water
model.
The
costs
include
the
pipes
and
valves
associated
with
GAC
contactors,
regeneration
furnace,
and
booster
pumps.

For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
Pipes
and
Valves
($)
=
81744
×
(
Design
Flow)
0.7327
For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
Pipes
and
Valves
($)
=
104596
×
(
Design
Flow)
0.7701
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
Pipes
and
Valves
($)
=
106594
×
(
Design
Flow)
0.7674
For
small
and
very
small
systems,
the
capital
costs
for
pipes
and
valves
were
included
in
the
GAC
package
costs.

Electrical
Costs
For
large
systems,
the
electrical
capital
costs
are
obtained
from
the
Water
model.
These
costs
included
flow
measurement
and
instrumentation,
and
master
operations
control
panel.

For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
Electrical
($)
=
25862
×
(
Design
Flow)
0.7329
For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
Electrical
($)
=
32569
×
(
Design
Flow)
0.7623
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
Electrical
($)
=
34188
×
(
Design
Flow)
0.7554
For
small
and
very
small
systems,
the
capital
costs
for
electrical
control
panels
were
included
in
the
GAC
package
costs.

Process
Monitoring
Equipment
Costs
The
performance
of
GAC
in
removing
DBP
can
be
measured
by
monitoring
the
amount
of
TOC
or
DOC
removed
by
the
GAC
column.
Regular
monitoring
for
TOC
will
also
enable
the
detection
of
any
unexpected
breakthrough.
For
large
systems,
it
was
assumed
that
TOC
monitoring
will
be
conducted
in­
house;
therefore,
two
TOC
analyzers
will
be
purchased.
For
small
systems,
it
was
assumed
that
samples
will
be
sent
to
contracted
laboratories
for
TOC
measurement;
therefore,
TOC
analyzers
will
not
be
purchased.
Costs
were
obtained
from
vendor
quotes.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
89
Booster
Pump
Costs
A
booster
pump
system
is
included
to
overcome
additional
head
loss
introduced
by
the
GAC
system.
For
design
flows
greater
than
1
mgd,
the
capital
costs
for
the
booster
pump
system
were
obtained
from
the
Water
model.
These
costs
were
projected
to
0.1
mgd
using
a
straight
line.
The
assumption
in
the
model
was
a
horizontal
centrifugal
pump
capable
of
providing
up
to
100
feet
of
head.
For
design
flows
less
than
0.1
mgd,
estimates
from
vendors
were
used
to
determine
capital
costs
for
an
in­
line
centrifugal
pump.

For
design
flow
>
0.1
mgd:
Booster
Pump
($)
=
20913
×
(
Design
Flow)
0.7543
For
design
flow
<
0.1
mgd:
Booster
Pump
($)
=
665970
×
(
Design
Flow)
2
 
13682
×
(
Design
Flow)
+
829.1
Capital
Cost
Multipliers
The
total
direct
costs
were
estimated
by
multiplying
the
subtotal
of
process
costs
by
1.67
for
small
systems
(
design
flow
less
than
1
mgd)
and
2.0
for
large
systems
(
design
flow
greater
than
1
mgd).
The
capital
cost
multiplier
includes
percentages
for
process
installation,
site
work,
contractor
overhead
and
profit,
contingencies,
engineering
and
design,
mobilization
and
bonding,
legal
and
administrative,
and
interest
during
construction.
See
Exhibit
4.2
for
the
percentages
of
each
that
make
up
the
multiplier.

Indirect
Capital
Costs
The
indirect
capital
costs
for
all
systems
include
housing,
piloting,
permitting,
land,
and
operator
training.

Housing
Costs
For
design
flows
greater
than
1
mgd,
a
building
cost
was
assumed
to
house
the
process
equipment.
The
process
costs
estimated
in
the
previous
steps
do
not
include
the
cost
of
the
building.
The
building
cost
was
assumed
to
be
a
function
of
the
process
area.
The
process
area
was
obtained
from
the
Water
model.

Process
Area
(
sq
ft)
=
681.18
×
(
Design
Flow)
0.612
Housing
($)
=
48.95
×
Process
Area
Additional
housing
was
not
assumed
to
be
needed
for
small
systems.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
90
Piloting
Costs
It
was
assumed
that
pilot­
scale
or
bench­
scale
tests
would
be
necessary
to
determine
the
capacity
of
GAC
to
remove
DBP
precursors
(
TOC
or
DOC)
for
a
particular
type
of
water.
Piloting
costs
were
assumed
to
be
$
5,000
for
design
flow
less
than
0.1
mgd,
$
10,000
for
design
flow
greater
than
0.1
mgd
but
less
than
1.0
mgd,
and
$
50,000
for
design
flow
greater
than
1.0
mgd.

Permitting
Costs
Permitting
costs
were
assumed
for
all
system
sizes.
Permitting
was
estimated
at
three
percent
of
the
total
process
cost
(
i.
e.,
pre­
capital
cost
multiplier).
A
minimum
permitting
cost
of
$
2,500
and
a
maximum
of
$
500,000
was
also
assumed.
For
further
details
about
these
costs,
refer
to
section
4.2.

Land
Costs
Land
costs
were
assumed
to
be
two
percent
of
the
total
capital
cost
for
all
system
sizes.
For
further
details
about
these
costs,
refer
to
section
4.2.

Operator
Training
Costs
While
the
operators
from
large
systems
generally
undergo
regular
training,
the
operators
from
small
systems
may
require
additional
training.
For
design
flow
less
than
1
mgd,
it
was
assumed
that
one
operator
will
be
trained
on
GAC
treatment
process
for
three
days
at
a
cost
of
approximately
$
500
($
25
per
hour).

4.5.1.2
Summary
of
GAC
O&
M
Cost
Assumptions
GAC
Usage
Rate
and
Replacement
Costs
For
design
flows
greater
than
10
mgd
and
in
the
0.1­
1
mgd
range,
the
annual
GAC
usage
rate
(
lbs/
year)
was
calculated
from
average
flow,
EBCT,
and
number
of
regenerations
per
year.
The
annual
GAC
replacement
costs
were
based
on
a
unit
cost
that
declines
with
higher
quantities
of
GAC.
The
unit
cost
ranged
from
$
1.00
to
$
1.20
per
pound.
For
design
flows
between
1
and
10
mgd,
the
annual
GAC
replacement
costs
were
obtained
by
linear
interpolation
between
the
costs
for
1
mgd
and
10
mgd
systems.
For
design
flows
less
than
0.1
mgd,
the
annual
GAC
replacement
costs
were
not
listed
separately
but
were
included
in
the
total
O&
M
costs
obtained
from
the
VSS
model.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
91
For
design
flow
<
1
mgd
For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
GAC
Replacement
($/
yr)
=
33034
×
(
Average
Flow)
+
111.2
For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
GAC
Replacement
($/
yr)
=
98716
×
(
Average
Flow)
+
344.55
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
GAC
Replacement
($/
yr)
=
260881
×
(
Average
Flow)
+
795.77
For
design
flow
>
1
mgd
and
<
10
mgd
For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
GAC
Replacement
($/
yr)
=
926.57
×
(
Average
Flow)
+
11693
For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
GAC
Replacement
($/
yr))
=
2774.2
×
(
Average
Flow)
+
34957
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
GAC
Replacement
($/
yr)
=
7266.7
×
(
Average
Flow)
+
92267
For
design
flow
>
10
mgd
For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
GAC
Replacement
($/
yr)
=
3146.3
×
(
Average
Flow)
+
4073.3
For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
GAC
Replacement
($/
yr)
=
9440.3
×
(
Average
Flow)
+
11853
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
GAC
Replacement
($/
yr)
=
25190
×
(
Average
Flow)
+
27754
Labor
Costs
For
design
flows
greater
than
10
mgd,
the
annual
labor
hours
were
obtained
from
the
Water
model.
The
labor
hours
include
the
requirements
associated
with
operation
of
GAC
contactors,
media
replacement,
regeneration
furnace,
and
booster
pumps.

For
design
flows
between
0.1­
1
mgd,
the
annual
labor
hours
were
obtained
from
the
Water
model.
For
this
model,
the
labor
hours
included
requirements
associated
with
operation
of
the
GAC
package
unit,
media
replacement,
and
booster
pumps.
For
design
flows
between
1
and
10
mgd,
the
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
92
annual
labor
hours
were
obtained
by
linear
interpolation
between
the
labor
hours
for
1
mgd
and
10
mgd
systems.

For
the
very
small
systems
(
design
flows
<
0.1
mgd),
labor
requirements
were
assumed
to
be
one
hour
per
week
plus
an
additional
8
hours
per
reactivation.
However,
the
annual
labor
hours
were
not
listed
separately
but
were
included
in
the
total
O&
M
costs
obtained
from
the
VSS
model.

The
annual
labor
costs
for
all
flow
rates
were
obtained
by
multiplying
the
labor
hours
by
unit
labor
costs
of
$
24.96
per
hour.

For
design
flow
<
1
mgd
For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
Labor
($/
yr)
=
((
858.36
×
Average
Flow)
+
402.56)
×
24.96)

For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
Labor
($/
yr)
=
((
1503.2
×
Average
Flow)
+
433.84)
×
24.96
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
Labor
($/
yr)
=
((
1503.2
×
Average
Flow)
+
433.84)
×
24.96
For
design
flow
>
1
mgd
and
<
10
mgd
For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
Labor
($/
yr)
=
((
551.97
×
Average
Flow)
+
533.12
)
×
24.96
For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
Labor
($/
yr)
=
((
683.86
×
Average
Flow)
+
709.64)
×
24.96
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
Labor
($/
yr)
=
((
810.91
×
Average
Flow)
+
663.91)
×
24.96
For
design
flow
>
10
mgd
For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
Labor
($/
yr)
=
(
143.15
×
Average
Flow)
+
2538.7)
×
24.96
For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
Labor
($/
yr)
=
((­
0.2147
×
Average
Flow2)
+
(
343.74
×
Average
Flow)
+
2100)
×
24.96
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
Labor
($/
yr)
=
(
1297.2
×
Average
Flow0.7536)
×
24.96
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
93
Power
(
Electricity)
Costs
For
design
flows
greater
than
10
mgd,
the
annual
power
requirements
(
kWh/
year)
were
obtained
from
the
Water
model.
For
this
model,
the
power
requirements
included
those
associated
with
operation
of
GAC
contactors,
media
replacement,
regeneration
furnace,
and
booster
pumps.

For
design
flows
between
0.1­
1
mgd,
the
annual
power
requirements
were
obtained
from
the
Water
model.
For
this
model,
the
power
requirements
included
those
associated
with
operation
of
GAC
package
unit
and
booster
pumps.

For
design
flows
between
1
and
10
mgd,
the
annual
power
requirements
were
obtained
by
linear
interpolation
between
the
power
requirements
for
1
mgd
and
10
mgd
systems.

For
the
very
small
systems
(
design
flows
<
0.1
mgd),
the
annual
power
costs
were
not
listed
separately
but
were
included
in
the
total
O&
M
costs
obtained
from
the
VSS
model.

The
annual
power
costs
were
obtained
by
multiplying
the
energy
requirements
(
kWh/
year)
by
unit
energy
costs
of
$
0.076
per
kWh.

For
design
flow
<
1
mgd
For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
Power
($/
yr))
=
(
240221
×
Average
Flow)
+
71518)
×
0.076
For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
Power
($/
yr)
=
(
276311
×
Average
Flow0.3872)
×
0.076
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
Power
($/
yr)
=
(
276311
×
Average
Flow0.3872)
×
0.076
For
design
flow
>
1
mgd
and
<
10
mgd
For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
Power
($/
yr))
=
((
74235
×
Average
Flow)
+
127519)
×
0.076
For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
Power
($/
yr)
=
((
99122
×
Average
Flow)
+
149023)
×
0.076
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
Power
($/
yr)
=
((
127743
×
Average
Flow)
+
138719)
×
0.076
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
94
For
design
flow
>
10
mgd
For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
Power
($/
yr)
=
((
73380
×
Average
Flow)
+
215530)
×
0.076
For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
Power
($/
yr)
=
((
75925
×
Average
Flow)
+
329950)
×
0.076
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
Power
($/
yr)
=
((
79096
×
Average
Flow)
+
410520)
×
0.076
Natural
Gas
Costs
For
design
flows
greater
than
1
mgd,
the
natural
gas
requirements
(
cubic
feet/
year)
associated
with
the
regeneration
furnace
were
obtained
from
the
Water
model.
The
annual
costs
for
natural
gas
were
obtained
by
multiplying
the
gas
requirements
(
cubic
feet/
year)
by
unit
gas
costs
of
$
0.006
per
cubic
feet.

For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
Natural
Gas
($/
yr)
=
(
510552
×
Average
Flow0.84)
×
0.006
For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
Natural
Gas
($/
yr)
=
(
1000000
×
Average
Flow0.853)
×
0.006
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
Natural
Gas
($/
yr)
=
(
3000000
×
Average
Flow0.8702)
×
0.006
Performance
Monitoring
Costs
For
design
flows
less
than
1
mgd,
the
number
of
TOC
samples
were
based
on
analyzing
one
sample
every
two
weeks
per
GAC
pressure
vessel.
Performance
monitoring
costs
were
based
on
the
assumption
that
the
samples
will
be
sent
to
contract
laboratories
and
that
the
cost
of
TOC
analyses
are
$
65
per
sample.

For
design
flows
greater
than
1
mgd,
it
was
assumed
that
the
TOC
samples
will
be
analyzed
inhouse
using
the
automated
TOC
analyzers.
Therefore,
no
additional
performance
monitoring
costs
were
assumed
for
this
system
size.

Maintenance
Materials
Costs
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
95
For
design
flows
greater
than
10
mgd,
the
maintenance
materials
costs
were
obtained
from
the
Water
model.
For
this
model,
the
maintenance
materials
included
those
associated
with
operation
of
GAC
contactors,
media
replacement,
regeneration
furnace,
and
booster
pumps.

For
design
flows
between
0.1­
1
mgd,
the
maintenance
materials
costs
were
obtained
from
the
Water
model.
For
this
model,
the
maintenance
materials
requirements
included
those
associated
with
operation
of
GAC
package
units
and
booster
pumps.

For
design
flows
between
1
and
10
mgd,
the
maintenance
materials
costs
were
obtained
by
linear
interpolation
between
the
power
requirements
for
1
mgd
and
10
mgd
systems.
For
the
very
small
systems
(
design
flows
<
0.1
mgd),
the
maintenance
materials
costs
were
not
listed
separately
but
included
in
the
total
O&
M
costs
obtained
from
the
VSS
model.

For
design
flow
<
1
mgd
For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
Materials
($/
yr)
=
(
6702.4
×
Average
Flow)
+
626.84
For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
Materials
($/
yr)
=
(
12444
×
Average
Flow)
+
898.16
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
Materials
($/
yr)
=
(
12444
×
Average
Flow)
+
898.16
For
design
flow
>
1
mgd
and
<
10
mgd
For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
Materials
($/
yr)
=
(
1390.1
×
Average
Flow)
+
2637.4
For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
Materials
($/
yr)
=
(
2708.8
×
Average
Flow)
+
4333.4
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
Materials
($/
yr)
=
(
3529.2
×
Average
Flow)
+
4038
For
design
flow
>
10
mgd
For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
Materials
($/
yr)
=
3458.7
×
Average
Flow0.6551
For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
Materials
($/
yr)
=
6202.7
×
Average
Flow0.641
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
96
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
Materials
($/
yr)
=
7750.8
×
Average
Flow0.6105
VSS
Model
Costs
For
the
very
small
systems
(
design
flows
<
0.1
mgd),
the
total
O&
M
costs
were
obtained
from
the
VSS
model.
These
costs
include
operation
of
GAC
pressure
vessels
and
booster
pumps,
material
replacement,
labor,
and
power.

For
EBCT
10
min
and
Reactivation
Frequency
=
360
days:
VSS
Model
($/
yr)
=
144625
×
Average
Flow0.5907
For
EBCT
20
min
and
Reactivation
Frequency
=
240
days:
VSS
Model
($/
yr)
=
231094
×
Average
Flow0.6421
For
EBCT
20
min
and
Reactivation
Frequency
=
90
days:
VSS
Model
($/
yr)
=
607295
×
Average
Flow0.7075
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
97
Design
Flow
(
mgd)
0.007
0.022
0.037
0.091
0.18
0.27
0.36
0.68
1.0
Average
Flow
(
mgd)
0.0015
0.0054
0.0095
0.025
0.054
0.084
0.11
0.23
0.35
CAPITAL
COST
SUMMARY
TOTAL
CAPITAL
COST
$
60,750
$
97,307
$
153,426
$
206,628
$
258,604
$
434,477
$
753,229
INDIRECT
CAPITAL
COSTS
$
9,034
$
9,872
$
17,306
$
19,839
$
22,314
$
30,689
$
83,963
Process
area
(
sq
ft)
Housing
Piloting
$
5,000
$
5,000
$
10,000
$
10,000
$
10,000
$
10,000
$
50,000
Permitting
$
2,500
$
2,623
$
4,084
$
5,604
$
7,089
$
12,114
$
20,078
Land
$
1,034
$
1,749
$
2,722
$
3,736
$
4,726
$
8,076
$
13,385
Operator
Training
$
500
$
500
$
500
$
500
$
500
$
500
$
500
WITH
CAPITAL
COST
MULTIPLIER
$
51,716
$
87,435
$
136,120
$
186,789
$
236,289
$
403,788
$
669,265
SUBTOTAL
PROCESS
COST
$
30,968
$
52,356
$
81,509
$
111,850
$
141,491
$
241,789
$
334,633
Nos
of
GAC
contactors
in
use
2
2
4
4
5
5
5
GAC
Contactor,
Media,
&
Regeneration
Furnace
***
***
***
***
***
***
***
GAC
Package
Unit
(
for
small
systems)
$
29,744
$
47,305
$
75,825
$
104,132
$
131,903
$
226,299
$
313,913
Pipes
and
Valves
***
***
***
***
***
***
***
Electrical
(
Instrumentaion
&
Controls)
***
***
***
***
***
***
***
Process
Monitoring
Equipment
(
TOC
***
***
***
***
***
***
***
Booster
Pumps
$
1,223
$
5,052
$
5,684
$
7,717
$
9,587
$
15,490
$
20,720
O
&
M
SUMMARY
TOTAL
O&
M
COST
PER
YEAR
$
12,360
$
19,485
$
28,052
$
30,902
$
34,917
$
46,132
$
57,232
GAC
Replacement
(
lbs/
yr)
***
***
1895
2886
3745
7709
11673
GAC
Replacement
($/
yr)
$
2,859
$
4,289
$
5,513
$
11,047
$
16,466
Labor
(
hr/
yr)
***
***
449
475
497
600
703
Labor
($/
yr)
$
11,205
$
11,848
$
12,405
$
14,976
$
17,547
Power
(
kWh/
yr)
***
***
84,490
91,697
97,942
126,769
155,595
Power
($/
yr)
$
6,759
$
7,336
$
7,835
$
10,142
$
12,448
Natural
Gas
(
cu
ft/
yr)
***
***
***
***
***
***
***
Natural
Gas
($/
yr)
TOC
measurement
(
samples/
year)
48
48
96
96
120
120
120
Performance
Monitoring
($/
yr)
$
3,120
$
3,120
$
6,240
$
6,240
$
7,800
$
7,800
$
7,800
Maintenance
Materials
($/
yr)
***
***
$
989
$
1,190
$
1,364
$
2,168
$
2,973
Total
O&
M
costs
(
from
VSS
Model)
­
$/
yr
$
9,240
$
16,365
***
***
***
***
***
Exhibit
4.46:
Summary
of
GAC
Costs
(
EBCT
=
10
minutes,
360
day
reactivation
frequency)

Note:
***
=
N/
A
Source:
Section
4.5.1
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
98
Design
Flow
(
mgd)
1.2
2
3.5
7
17
22
76
210
430
520
Average
Flow
(
mgd)
0.41
0.77
1.4
3
7.8
11
38
120
270
350
CAPITAL
COST
SUMMARY
TOTAL
CAPITAL
COST
$
961,218
$
1,331,550
$
1,935,301
$
3,129,311
$
5,894,486
$
7,103,058
$
17,577,650
$
36,661,251
$
61,958,498
$
71,251,757
INDIRECT
CAPITAL
COSTS
$
128,896
$
159,561
$
208,135
$
301,112
$
508,138
$
596,426
$
1,334,309
$
2,120,273
$
3,090,983
$
3,438,096
Process
area
(
sq
ft)
762
1,041
1,466
2,241
3,857
4,517
9,645
17,966
27,858
31,294
Housing
$
37,280
$
50,962
$
71,777
$
109,702
$
188,821
$
221,094
$
472,142
$
879,453
$
1,363,632
$
1,531,823
Piloting
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
Permitting
$
24,970
$
35,160
$
51,815
$
84,846
$
161,590
$
195,199
$
487,300
$
500,000
$
500,000
$
500,000
Land
$
16,646
$
23,440
$
34,543
$
56,564
$
107,727
$
130,133
$
324,867
$
690,820
$
1,177,350
$
1,356,273
Operator
Training
WITH
CAPITAL
COST
MULTIPLIER
$
832,322
$
1,171,989
$
1,727,166
$
2,828,199
$
5,386,348
$
6,506,633
$
16,243,341
$
34,540,978
$
58,867,516
$
67,813,660
SUBTOTAL
PROCESS
COST
$
416,161
$
585,994
$
863,583
$
1,414,099
$
2,693,174
$
3,253,316
$
8,121,670
$
17,270,489
$
29,433,758
$
33,906,830
Nos
of
GAC
contactors
in
use
5
5
5
10
10
10
10
20
20
20
GAC
Contactor,
Media,
&
Regeneration
Furnace
$
220,999
$
324,338
$
493,764
$
830,985
$
1,618,049
$
1,963,740
$
4,982,135
$
10,688,361
$
18,308,774
$
21,117,522
GAC
Package
Unit
(
for
small
systems)
***
***
***
***
***
***
***
***
***
***
Pipes
and
Valves
$
92,564
$
134,583
$
202,798
$
336,999
$
645,617
$
779,863
$
1,934,181
$
4,073,006
$
6,886,005
$
7,914,813
Electrical
(
Instrumentaion
&
Controls)
$
29,286
$
42,585
$
64,177
$
106,660
$
204,375
$
246,884
$
612,462
$
1,289,988
$
2,181,224
$
2,507,206
Process
Monitoring
Equipment
(
TOC
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
Booster
Pumps
$
23,775
$
34,950
$
53,306
$
89,917
$
175,595
$
213,292
$
543,354
$
1,169,595
$
2,008,217
$
2,317,751
O
&
M
SUMMARY
TOTAL
O&
M
COST
PER
YEAR
$
51,976
$
61,522
$
77,734
$
117,714
$
223,726
$
276,141
$
700,590
$
1,930,628
$
4,109,268
$
5,253,236
GAC
Replacement
(
lbs/
yr)
12073
12406
12990
14473
28614
38683
123633
381629
853574
1105278
GAC
Replacement
($/
yr)
$
17,007
$
17,459
$
18,248
$
20,246
$
38,974
$
52,056
$
158,605
$
466,311
$
1,005,806
$
1,286,948
Labor
(
hr/
yr)
759
958
1306
2189
3655
4113
7978
19717
41189
52641
Labor
($/
yr)
$
18,955
$
23,915
$
32,595
$
54,638
$
91,236
$
102,669
$
199,141
$
492,129
$
1,028,082
$
1,313,924
Power
(
kWh/
yr)
157,955
184,680
231,448
350,224
787,894
1,022,710
3,003,970
9,021,130
20,028,130
25,898,530
Power
($/
yr)
$
12,636
$
14,774
$
18,516
$
28,018
$
63,032
$
81,817
$
240,318
$
721,690
$
1,602,250
$
2,071,882
Natural
Gas
(
cu
ft/
yr)
241423
409913
677310
1284759
2866814
3826572
10840722
28480803
56284076
69993408
Natural
Gas
($/
yr)
$
1,449
$
2,459
$
4,064
$
7,709
$
17,201
$
22,959
$
65,044
$
170,885
$
337,704
$
419,960
TOC
measurement
(
samples/
year)
***
***
***
***
***
***
***
***
***
***
Performance
Monitoring
($/
yr)
Maintenance
Materials
($/
yr)
$
1,929
$
2,914
$
4,312
$
7,104
$
13,284
$
16,639
$
37,483
$
79,613
$
135,425
$
160,521
Total
O&
M
costs
(
from
VSS
Model)
­
$/
yr
***
***
***
***
***
***
***
***
***
***
Exhibit
4.46
(
continued):
Summary
of
GAC
Costs
(
EBCT
=
10
minutes,
360
day
reactivation
frequency)

Note:
***
=
N/
A
Source:
Section
4.5.1
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
99
Design
Flow
(
mgd)
0.007
0.022
0.037
0.091
0.18
0.27
0.36
0.68
1.0
Average
Flow
(
mgd)
0.0015
0.0054
0.0095
0.025
0.054
0.084
0.11
0.23
0.35
CAPITAL
COST
SUMMARY
TOTAL
CAPITAL
COST
$
34,944
$
51,211
$
67,885
$
132,410
$
232,148
$
326,766
$
417,447
$
708,992
$
1,179,491
INDIRECT
CAPITAL
COSTS
$
8,528
$
8,847
$
9,174
$
11,543
$
21,055
$
25,560
$
29,878
$
43,762
$
104,261
Process
area
(
sq
ft)
Housing
Piloting
$
5,000
$
5,000
$
5,000
$
5,000
$
10,000
$
10,000
$
10,000
$
10,000
$
50,000
Permitting
$
2,500
$
2,500
$
2,500
$
3,626
$
6,333
$
9,036
$
11,627
$
19,957
$
32,257
Land
$
528
$
847
$
1,174
$
2,417
$
4,222
$
6,024
$
7,751
$
13,305
$
21,505
Operator
Training
$
500
$
500
$
500
$
500
$
500
$
500
$
500
$
500
$
500
WITH
CAPITAL
COST
MULTIPLIER
$
26,416
$
42,364
$
58,711
$
120,866
$
211,093
$
301,206
$
387,568
$
665,231
$
1,075,230
SUBTOTAL
PROCESS
COST
$
15,818
$
25,368
$
35,156
$
72,375
$
126,403
$
180,363
$
232,077
$
398,342
$
537,615
Nos
of
GAC
contactors
in
use
2
2
2
2
4
4
5
5
5
GAC
Contactor,
Media,
&
Regeneration
Furnace
***
***
***
***
***
***
***
***
***
GAC
Package
Unit
(
for
small
systems)
$
15,059
$
24,525
$
33,933
$
67,323
$
120,719
$
172,645
$
222,489
$
382,852
$
516,895
Pipes
and
Valves
***
***
***
***
***
***
***
***
***
Electrical
(
Instrumentaion
&
Controls)
***
***
***
***
***
***
***
***
***
Process
Monitoring
Equipment
(
TOC
Analyzer)
***
***
***
***
***
***
***
***
***
Booster
Pumps
$
759
$
843
$
1,223
$
5,052
$
5,684
$
7,717
$
9,587
$
15,490
$
20,720
O
&
M
SUMMARY
TOTAL
O&
M
COST
PER
YEAR
$
9,222
$
18,223
$
25,644
$
47,782
$
48,603
$
61,851
$
74,549
$
123,862
$
171,361
GAC
Replacement
(
lbs/
yr)
***
***
***
***
14883
22710
29493
60798
92104
GAC
Replacement
($/
yr)
$
20,798
$
31,216
$
40,122
$
80,331
$
119,625
Labor
(
hr/
yr)
***
***
***
***
515
560
599
780
960
Labor
($/
yr)
$
12,855
$
13,980
$
14,956
$
19,458
$
23,961
Power
(
kWh/
yr)
***
***
***
***
89,244
105,896
117,551
156,408
184,018
Power
($/
yr)
$
7,140
$
8,472
$
9,404
$
12,513
$
14,721
Natural
Gas
(
cu
ft/
yr)
***
***
***
***
***
***
***
***
***
Natural
Gas
($/
yr)
TOC
measurement
(
samples/
year)
48
48
48
48
96
96
120
120
120
Performance
Monitoring
($/
yr)
$
3,120
$
3,120
$
3,120
$
3,120
$
6,240
$
6,240
$
7,800
$
7,800
$
7,800
Maintenance
Materials
($/
yr)
***
***
***
***
$
1,570
$
1,943
$
2,267
$
3,760
$
5,254
Total
O&
M
costs
(
from
VSS
Model)
­
$/
yr
$
6,102
$
15,103
$
22,524
$
44,662
***
***
***
***
***
Exhibit
4.47:
Summary
of
GAC
Costs
(
EBCT
=
20
minutes,
90
day
reactivation
frequency)

Note:
***
=
N/
A
Source:
Section
4.5.1
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
100
Design
Flow
(
mgd)
1.2
2
3.5
7
17
22
76
210
430
520
Average
Flow
(
mgd)
0.41
0.77
1.4
3
7.8
11
38
120
270
350
CAPITAL
COST
SUMMARY
TOTAL
CAPITAL
COST
$
1,491,296
$
2,117,739
$
3,146,100
$
5,196,469
$
9,994,133
$
12,105,188
$
30,250,612
$
64,392,745
$
110,161,213
$
127,064,791
INDIRECT
CAPITAL
COSTS
$
181,926
$
235,771
$
321,625
$
487,224
$
859,504
$
1,019,256
$
2,020,399
$
3,485,977
$
5,343,940
$
6,011,591
Process
area
(
sq
ft)
1,358
1,873
2,664
4,122
7,207
8,477
18,504
35,094
55,109
62,115
Housing
$
66,457
$
91,673
$
130,401
$
201,762
$
352,773
$
414,959
$
905,795
$
1,717,842
$
2,697,595
$
3,040,527
Piloting
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
Permitting
$
39,281
$
56,459
$
84,734
$
141,277
$
274,039
$
332,578
$
500,000
$
500,000
$
500,000
$
500,000
Land
$
26,187
$
37,639
$
56,490
$
94,185
$
182,693
$
221,719
$
564,604
$
1,218,135
$
2,096,345
$
2,421,064
Operator
Training
WITH
CAPITAL
COST
MULTIPLIER
$
1,309,370
$
1,881,968
$
2,824,475
$
4,709,244
$
9,134,629
$
11,085,933
$
28,230,212
$
60,906,768
$
104,817,273
$
121,053,200
SUBTOTAL
PROCESS
COST
$
654,685
$
940,984
$
1,412,238
$
2,354,622
$
4,567,314
$
5,542,966
$
14,115,106
$
30,453,384
$
52,408,637
$
60,526,600
Nos
of
GAC
contactors
in
use
5
5
5
10
10
10
10
20
20
20
GAC
Contactor,
Media,
&
Regeneration
Furnace
$
421,030
$
619,548
$
945,933
$
1,597,714
$
3,125,370
$
3,798,185
$
9,698,560
$
20,916,945
$
35,963,742
$
41,521,951
GAC
Package
Unit
(
for
small
systems)
***
***
***
***
***
***
***
***
***
***
Pipes
and
Valves
$
121,469
$
179,768
$
276,197
$
470,143
$
928,856
$
1,132,080
$
2,931,151
$
6,394,005
$
11,082,189
$
12,822,209
Electrical
(
Instrumentaion
&
Controls)
$
38,874
$
57,180
$
87,263
$
147,309
$
287,955
$
349,872
$
892,502
$
1,923,301
$
3,304,950
$
3,815,151
Process
Monitoring
Equipment
(
TOC
Analyzer)
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
Booster
Pumps
$
23,775
$
34,950
$
53,306
$
89,917
$
175,595
$
213,292
$
543,354
$
1,169,595
$
2,008,217
$
2,317,751
O
&
M
SUMMARY
TOTAL
O&
M
COST
PER
YEAR
$
177,461
$
198,999
$
235,875
$
327,328
$
649,586
$
854,448
$
2,426,385
$
6,675,323
$
13,806,859
$
17,448,504
GAC
Replacement
(
lbs/
yr)
95246
97862
102440
114067
224236
304844
984974
3050554
6829054
8844254
GAC
Replacement
($/
yr)
$
123,533
$
126,783
$
132,460
$
146,831
$
280,444
$
376,193
$
1,153,011
$
3,384,412
$
7,278,711
$
9,302,877
Labor
(
hr/
yr)
996
1288
1799
3097
6099
7903
20116
47850
88162
107205
Labor
($/
yr)
$
24,870
$
32,156
$
44,908
$
77,292
$
152,242
$
197,263
$
502,084
$
1,194,325
$
2,200,530
$
2,675,847
Power
(
kWh/
yr)
191,094
237,081
317,559
521,948
1,027,469
1,280,576
3,416,168
9,902,040
21,766,440
28,094,120
Power
($/
yr)
$
15,287
$
18,966
$
25,405
$
41,756
$
82,198
$
102,446
$
273,293
$
792,163
$
1,741,315
$
2,247,530
Natural
Gas
(
cu
ft/
yr)
1380911
2389712
4020517
7803909
17923465
24173591
71096618
193385886
391646277
490873138
Natural
Gas
($/
yr)
$
8,285
$
14,338
$
24,123
$
46,823
$
107,541
$
145,042
$
426,580
$
1,160,315
$
2,349,878
$
2,945,239
TOC
measurement
(
samples/
year)
***
***
***
***
***
***
***
***
***
***
Performance
Monitoring
($/
yr)
Maintenance
Materials
($/
yr)
$
5,485
$
6,755
$
8,979
$
14,626
$
27,163
$
33,506
$
71,417
$
144,108
$
236,425
$
277,013
Total
O&
M
costs
(
from
VSS
Model)
­
$/
yr
***
***
***
***
***
***
***
***
***
***
Exhibit
4.47
(
continued):
Summary
of
GAC
Costs
(
EBCT
=
20
minutes,
90
day
reactivation
frequency)

Note:
***
=
N/
A
Source:
Section
4.5.1
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
101
Design
Flow
(
mgd)
0.007
0.022
0.037
0.091
0.18
0.27
0.36
0.68
1.0
Average
Flow
(
mgd)
0.0015
0.0054
0.0095
0.025
0.054
0.084
0.11
0.23
0.35
CAPITAL
COST
SUMMARY
TOTAL
CAPITAL
COST
$
34,944
$
51,211
$
67,885
$
132,410
$
232,148
$
326,766
$
417,447
$
708,992
$
1,179,491
INDIRECT
CAPITAL
COSTS
$
8,528
$
8,847
$
9,174
$
11,543
$
21,055
$
25,560
$
29,878
$
43,762
$
104,261
Process
area
(
sq
ft)
Housing
Piloting
$
5,000
$
5,000
$
5,000
$
5,000
$
10,000
$
10,000
$
10,000
$
10,000
$
50,000
Permitting
$
2,500
$
2,500
$
2,500
$
3,626
$
6,333
$
9,036
$
11,627
$
19,957
$
32,257
Land
$
528
$
847
$
1,174
$
2,417
$
4,222
$
6,024
$
7,751
$
13,305
$
21,505
Operator
Training
$
500
$
500
$
500
$
500
$
500
$
500
$
500
$
500
$
500
WITH
CAPITAL
COST
MULTIPLIER
$
26,416
$
42,364
$
58,711
$
120,866
$
211,093
$
301,206
$
387,568
$
665,231
$
1,075,230
SUBTOTAL
PROCESS
COST
$
15,818
$
25,368
$
35,156
$
72,375
$
126,403
$
180,363
$
232,077
$
398,342
$
537,615
Nos
of
GAC
contactors
in
use
2
2
2
2
4
4
5
5
5
GAC
Contactor,
Media,
&
Regeneration
Furnace
***
***
***
***
***
***
***
***
***
GAC
Package
Unit
(
for
small
systems)
$
15,059
$
24,525
$
33,933
$
67,323
$
120,719
$
172,645
$
222,489
$
382,852
$
516,895
Pipes
and
Valves
***
***
***
***
***
***
***
***
***
Electrical
(
Instrumentaion
&
Controls)
***
***
***
***
***
***
***
***
***
Process
Monitoring
Equipment
(
TOC
Analyzer)
***
***
***
***
***
***
***
***
***
Booster
Pumps
$
759
$
843
$
1,223
$
5,052
$
5,684
$
7,717
$
9,587
$
15,490
$
20,720
O
&
M
SUMMARY
TOTAL
O&
M
COST
PER
YEAR
$
6,673
$
11,206
$
14,742
$
24,752
$
36,031
$
42,959
$
50,255
$
75,195
$
98,890
GAC
Replacement
(
lbs/
yr)
***
***
***
***
5675
8637
11203
23049
34895
GAC
Replacement
($/
yr)
$
8,227
$
12,323
$
15,828
$
31,664
$
47,154
Labor
(
hr/
yr)
***
***
***
***
515
560
599
780
960
Labor
($/
yr)
$
12,855
$
13,980
$
14,956
$
19,458
$
23,961
Power
(
kWh/
yr)
***
***
***
***
89,244
105,896
117,551
156,408
184,018
Power
($/
yr)
$
7,140
$
8,472
$
9,404
$
12,513
$
14,721
Natural
Gas
(
cu
ft/
yr)
***
***
***
***
***
***
***
***
***
Natural
Gas
($/
yr)
TOC
measurement
(
samples/
year)
48
48
48
48
96
96
120
120
120
Performance
Monitoring
($/
yr)
$
3,120
$
3,120
$
3,120
$
3,120
$
6,240
$
6,240
$
7,800
$
7,800
$
7,800
Maintenance
Materials
($/
yr)
***
***
***
***
$
1,570
$
1,943
$
2,267
$
3,760
$
5,254
Total
O&
M
costs
(
from
VSS
Model)
­
$/
yr
$
3,553
$
8,086
$
11,622
$
21,632
***
***
***
***
***
Exhibit
4.48:
Summary
of
GAC
Costs
(
EBCT
=
20
minutes,
240
day
reactivation
frequency)

Note:
***
=
N/
A
Source:
Section
4.5.1
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
102
Design
Flow
(
mgd)
1.2
2
3.5
7
17
22
76
210
430
520
Average
Flow
(
mgd)
0.41
0.77
1.4
3
7.8
11
38
120
270
350
CAPITAL
COST
SUMMARY
TOTAL
CAPITAL
COST
$
1,299,190
$
1,855,588
$
2,780,301
$
4,651,079
$
9,110,253
$
11,096,119
$
28,529,679
$
62,098,782
$
107,964,358
$
125,068,321
INDIRECT
CAPITAL
COSTS
$
158,193
$
204,326
$
279,067
$
425,947
$
763,932
$
911,168
$
1,883,588
$
3,296,933
$
5,133,225
$
5,801,272
Process
area
(
sq
ft)
1,045
1,466
2,125
3,364
6,060
7,189
16,357
32,092
51,616
58,548
Housing
$
51,143
$
71,762
$
104,005
$
164,690
$
296,616
$
351,920
$
800,666
$
1,570,896
$
2,526,602
$
2,865,931
Piloting
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
$
50,000
Permitting
$
34,230
$
49,538
$
75,037
$
126,754
$
250,390
$
305,549
$
500,000
$
500,000
$
500,000
$
500,000
Land
$
22,820
$
33,025
$
50,025
$
84,503
$
166,926
$
203,699
$
532,922
$
1,176,037
$
2,056,623
$
2,385,341
Operator
Training
WITH
CAPITAL
COST
MULTIPLIER
$
1,140,997
$
1,651,263
$
2,501,234
$
4,225,132
$
8,346,321
$
10,184,951
$
26,646,091
$
58,801,849
$
102,831,133
$
119,267,049
SUBTOTAL
PROCESS
COST
$
570,499
$
825,631
$
1,250,617
$
2,112,566
$
4,173,160
$
5,092,476
$
13,323,046
$
29,400,924
$
51,415,567
$
59,633,524
Nos
of
GAC
contactors
in
use
5
5
5
10
10
10
10
11
12
13
GAC
Contactor,
Media,
&
Regeneration
Furnace
$
340,856
$
509,681
$
791,982
$
1,367,119
$
2,749,849
$
3,368,987
$
8,944,087
$
19,915,314
$
35,020,875
$
40,675,366
GAC
Package
Unit
(
for
small
systems)
***
***
***
***
***
***
***
***
***
***
Pipes
and
Valves
$
119,251
$
176,729
$
271,939
$
463,761
$
918,444
$
1,120,170
$
2,910,039
$
6,365,394
$
11,053,969
$
12,796,122
Electrical
(
Instrumentaion
&
Controls)
$
37,079
$
54,733
$
83,853
$
142,230
$
279,734
$
340,488
$
876,027
$
1,901,084
$
3,282,967
$
3,794,748
Process
Monitoring
Equipment
(
TOC
Analyzer)
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
$
49,538
Booster
Pumps
$
23,775
$
34,950
$
53,306
$
89,917
$
175,595
$
213,292
$
543,354
$
1,169,595
$
2,008,217
$
2,317,751
O
&
M
SUMMARY
TOTAL
O&
M
COST
PER
YEAR
$
96,841
$
110,105
$
133,014
$
190,387
$
361,906
$
463,435
$
1,278,749
$
3,580,415
$
7,445,710
$
9,260,140
GAC
Replacement
(
lbs/
yr)
36094
37093
38841
43280
85487
115696
370584
1144689
2560734
3315958
GAC
Replacement
($/
yr)
$
48,709
$
50,002
$
52,261
$
57,980
$
111,376
$
148,839
$
453,404
$
1,330,667
$
2,865,233
$
3,663,897
Labor
(
hr/
yr)
990
1236
1667
2761
4768
5855
14852
40257
79258
96108
Labor
($/
yr)
$
24,711
$
30,856
$
41,609
$
68,920
$
119,012
$
146,145
$
370,708
$
1,004,818
$
1,978,284
$
2,398,862
Power
(
kWh/
yr)
189,663
225,347
287,794
446,389
922,165
1,165,125
3,215,100
9,440,950
20,829,700
26,903,700
Power
($/
yr)
$
15,173
$
18,028
$
23,024
$
35,711
$
73,773
$
93,210
$
257,208
$
755,276
$
1,666,376
$
2,044,681
Natural
Gas
(
cu
ft/
yr)
467,417
800,160
1,332,439
2,552,610
5,767,090
7,732,287
22,261,550
59,366,522
118,564,122
147,941,508
Natural
Gas
($/
yr)
$
2,805
$
4,801
$
7,995
$
15,316
$
34,603
$
46,394
$
133,569
$
356,199
$
711,385
$
887,649
TOC
measurement
(
samples/
year)
***
***
***
***
***
***
***
***
***
***
Performance
Monitoring
($/
yr)
Maintenance
Materials
($/
yr)
$
5,444
$
6,419
$
8,126
$
12,460
$
23,143
$
28,848
$
63,859
$
133,455
$
224,432
$
265,050
Total
O&
M
costs
(
from
VSS
Model)
­
$/
yr
***
***
***
***
***
***
***
***
***
***
Exhibit
4.48
(
continued):
Summary
of
GAC
Costs
(
EBCT
=
20
minutes,
240
day
reactivation
frequency)

Note:
***
=
N/
A
Source:
Section
4.5.1
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
103
4.5.2
Nanofiltration
Nanofiltration
can
be
effective
for
the
control
of
DBP
precursors
(
i.
e.,
NOM),
as
well
as
microbial
contaminants.
NF
is
an
advanced
treatment
process
that
typically
requires
higher
levels
of
pre­
and
post­
treatment
than
traditional
water
treatment
processes.
The
costs
provided
in
this
section
assume
that
the
NF
system
is
an
"
add­
on"
polishing
treatment
process
for
an
existing
conventional
treatment
plant
generating
water
of
desired
quality
for
NF.
These
costs
do
not
include
any
additional
post­
treatments
that
may
be
necessary.
Costs
were
developed
assuming
a
feed
water
temperatures
of
10
°
C.
(
Costs
of
a
NF
system
can
vary
with
temperature.)

The
cost
estimates
assume
that
100
percent
of
the
flow
will
be
treated
by
the
NF
membranes
(
i.
e.,
no
blending).
Recovery
was
assumed
to
be
85
percent.
In
some
regions,
an
additional
cost
for
purchased
water
may
be
incurred
as
a
result
of
the
15
percent
water
loss.
The
costs
associated
with
these
losses
were
not
included
in
the
estimates
provided.

4.5.2.1
Summary
of
NF
Capital
Cost
Assumptions
Process
Costs
Capital
costs
were
estimated
based
on
vendor
quotations,
cost
estimating
guides,
and
best
professional
judgment
and
were
adjusted
to
year
2000
dollars
using
the
ENR
BCI.
Exhibit
4.54
presents
a
summary
of
line
item
capital
costs
for
retrofitting
NF
into
an
existing
treatment
plant
for
design
flows
ranging
from
0.007
mgd
to
520
mgd.
Costs
were
based
on
a
feed
water
temperature
of
10
°
C
and
a
recovery
of
85
percent.
The
spent
brine
was
assumed
to
be
directly
discharged
to
a
sewer,
storm
drain,
ocean
outfall,
or
a
salinity
interceptor.
The
methodology
used
for
estimating
capital
costs
is
discussed
in
this
section.

Membrane
System
Costs
Unlike
other
treatment
processes,
NF
systems
are
typically
supplied
by
equipment
vendors
as
package
skid­
mounted
units.
Vendors,
contacted
to
provide
cost
estimates,
provided
a
single
cost
estimate
that
included
the
following
items:

°
Membrane
skid
with
filter
housings
°
NF
membrane
elements
(
initial
batch)

°
Cartridge
pre­
filtration
°
System
feed
pumps
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
104
°
Acid
and
anti­
scalant
feed
systems
°
Clean­
in­
place
system
°
Instrumentation
and
controls
°
Pipes
and
valves
The
typical
percent
distribution
of
the
above
components
in
the
NF
equipment
cost
is
shown
in
Exhibit
4.49.
The
NF
skids
are
equipped
with
all
necessary
instrumentation
and
controls
and
pipes
and
valves;
therefore,
these
costs
were
included
as
part
of
the
NF
equipment
cost.

Exhibit
4.49:
Percent
Distribution
of
NF
Equipment
Cost
Capital
Cost
Item
NF
Equipment
Cost
(
as
%)

Membrane
skid
with
filter
housings
20%

NF
membrane
elements
(
initial
batch)
20%

Cartridge
pre­
filtration
10%

System
feed
pumps
12%

Acid
and
anti­
scalant
feed
systems
3%

Clean­
in­
place
system
5%

Instrumentation
and
controls
20%

Pipes
and
valves
10%

Sub­
Total
NF
Equipment
Cost
100%

Source:
Vendor
quotes
Online
Process
Monitoring
Equipment
Additional
process
monitoring
for
pH
and
turbidity
was
assumed
for
all
NF
systems.
Process
monitoring
equipment
includes
an
on­
line
conductivity/
pH
meter
($
2,500
for
meter
and
probe)
and
a
turbidimeter
($
2,500
for
meter
and
probe).
For
systems
smaller
than
2
mgd
capacity,
one
conductivity/
pH
meter
and
one
turbidimeter
were
assumed.
For
systems
larger
than
2
mgd,
the
number
of
meters
was
based
on
one
instrument
per
train/
skid.
Costs
were
obtained
from
vendor
quotes
and
were
adjusted
to
the
year
2000
dollars
using
the
ENR
BCI.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
105
Brine
Discharge
Pipeline
Costs
for
brine
discharge
include
construction
of
a
500­
foot
pipeline
from
the
NF
process
to
an
appropriate
sanitary
sewer
connector.
Pipe
material
was
assumed
to
be
PVC
or
reinforced
concrete
with
diameters
varying
from
2
to
24
inches
depending
on
the
quantity
of
water
to
be
discharged.
Costs
for
the
pipeline
were
obtained
from
Small
Water
System
Byproducts
Treatment
and
Disposal
Cost
Document
(
DPRA
1993a)
and
Water
System
Byproducts
Treatment
and
Disposal
Cost
Document
(
DPRA
1993b).
For
more
details
on
pipeline
costs
refer
to
section
4.4.5.

Capital
Cost
Multipliers
Total
direct
capital
costs
were
obtained
by
applying
a
capital
cost
multiplier
to
the
sum
of
all
process
costs.
The
capital
cost
multipliers
of
1.67
and
2.0
were
used
respectively
for
small
(<
2
mgd)
and
large
(>
2
mgd)
systems.
Unlike
other
treatment
processes,
membrane
systems
are
typically
supplied
by
the
equipment
vendor
as
package,
skid­
mounted
units;
therefore,
smaller
multipliers
were
used
compared
to
those
recommended
by
NDWAC.
For
more
discussion
on
the
multipliers
refer
to
section
4.2.1.

Indirect
Capital
Costs
Costs
for
permitting,
piloting,
membrane
housing,
land,
and
operator
training
were
totaled
and
are
referred
to
as
indirect
capital
costs
for
the
purposes
of
this
document.
Indirect
capital
costs
were
added
to
the
direct
capital
costs
to
obtain
total
capital
costs.

Permitting
Incorporating
NF
treatment
will
likely
require
coordination
with
the
appropriate
regulatory
agencies.
To
account
for
this,
permitting
costs
were
included
at
three
percent
of
the
process
cost.
A
minimum
permitting
fee
of
$
2,500
and
a
maximum
of
$
500,000
was
assumed.

Pilot
Testing
It
was
assumed
that
pilot­
or
bench­
scale
tests
would
be
necessary
to
ensure
compatibility
of
membrane
materials
with
process
chemicals
(
e.
g.,
coagulants
or
polymers),
as
well
as
to
determine
critical
design
parameters,
such
as
design
flux
and
cleaning
frequency.
Bench­
scale
flat
sheet
tests
were
assumed
for
systems
less
than
0.1
mgd,
at
a
cost
of
$
1,000.
Single­
element
tests
at
a
one­
time
cost
of
$
10,000
was
assumed
for
systems
between
0.1
and
1
mgd.
For
systems
larger
than
1
mgd,
three­
month
pilot
tests
at
a
cost
of
$
60,000
were
assumed.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
106
Membrane
Housing
Membrane
housing
costs
include
the
cost
for
a
building
to
house
the
membrane
skids
and
any
associated
appurtenances
(
e.
g.,
building
electrical,
HVAC,
and
lighting).
Housing
costs
will
vary
depending
on
size
of
the
system.
Exhibit
4.50
summarizes
the
membrane
housing
cost
assumptions
used
for
NF
costs.
A
range
of
housing
areas
from
900
to
1,100
ft2
per
mgd
was
assumed
with
a
minimum
of
100
ft2.
Housing
areas
are
based
on
experience
with
similar
systems.
A
unit
cost
of
$
48.95/
ft2
was
taken
from
RS
Means.
The
$
48.95/
ft2
unit
cost
assumes
a
factory
type
building.

Exhibit
4.50:
Summary
of
NF
Housing
Cost
Assumptions
System
Size
(
mgd)
Housing
Area1
<
10
mgd
1,100
ft2
per
mgd
>
10
mgd
900
ft2
per
mgd
Note:
1A
minimum
housing
area
of
100
ft2
was
also
assumed
for
very
small
systems.

Land
Land
cost
assumptions
for
NF
treatment
are
listed
in
Exhibit
4.51.
The
NDWAC
cost
working
group
recommended
a
factor
of
two
to
five
percent
of
capital
cost
for
land.
Previous
technology
cost
efforts
(
USEPA
2001)
adopted
land
costs
at
a
factor
of
five
percent
for
systems
less
than
1
mgd
and
two
percent
for
systems
greater
than
1
mgd;
however,
previous
cases
assumed
new
plant
construction,
instead
of
a
retrofit
which
was
assumed
in
this
document.
Using
a
two
to
five
percent
factor
for
land
resulted
in
unrealistic
costs
for
land
acquisition
($/
acre).
Therefore,
the
land
cost
factors
were
adjusted,
as
discussed
under
MF
cost
assumptions,
to
obtain
reasonable
costs.

Exhibit
4.51:
NF
Land
Cost
Assumptions
System
Design
Flow
(
mgd)
Land
Cost
(%
of
Total
Direct
Cost)

<
1
2%

1
­
10
1%

>
10
0.5%

Source:
Exhibit
4.7
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
107
Operator
Training
The
NDWAC
cost
working
group
also
recommended
inclusion
of
operator
training.
The
operator
training
costs
were
based
on
the
number
of
hours
required
per
system
size
to
train
an
operator.
Training
hours
are
based
on
experience
with
similar
systems.
Based
upon
system
size,
this
training
could
last
a
few
hours
or
a
few
days.
Exhibit
4.52
summarizes
the
operator
training
cost
assumptions
used
in
this
document.

Exhibit
4.52:
NF
Operator
Training
Cost
Assumptions
System
Design
Flow
(
mgd)
Training
Cost
($)

<
0.5
included
in
membrane
system
price
0.5
­
1
$
1,000
1
­
10
$
3,000
10
­
100
$
10,000
>
100
$
25,000
4.5.2.2
Summary
of
NF
O&
M
Cost
Assumptions
NF
O&
M
costs
were
estimated
using
current
plant
operational
data
and
industry
guidelines.
Exhibit
4.54
presents
a
summary
of
line
items
of
O&
M
costs.
This
section
discusses
the
assumptions
regarding
O&
M
estimates
presented
in
this
document.

Clean­
in­
Place
Chemicals
NF
systems
will
require
periodic
(
typically
quarterly
or
semi­
annually)
chemical
cleaning
to
remove
biological/
particulate
foulants
and
scalants
from
the
membrane
surfaces.
Membrane
cleaning
is
performed
using
manufacturer­
recommended
cleaning
agents,
and
costs
can
vary.
Based
on
discussions
with
manufacturers
and
experience
with
similar
systems,
a
typical
costs
of
$
0.01
per
1,000
gallons
of
water
produced
was
assumed
for
all
system
sizes
to
account
for
cleaning
chemical
costs.
Thus,
cleaning
chemical
costs
can
be
estimated
by
the
following
equation:

Cleaning
Chemicals
($/
yr)
=
0.01
×
Average
Flow
(
mgd)
×
1,000
×
365
A
minimum
cost
of
$
50/
year
was
assumed
for
cleaning
chemicals;
this
accounts
for
the
cost
of
purchasing
a
15­
gallon
pail
of
cleaning
chemical.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
108
Acid/
Anti­
Scalant
and
Caustic
Chemicals
Addition
of
acid
and
anti­
scalant
is
necessary
to
reduce
the
fouling
and
scaling
of
NF
membranes.
Caustic
may
be
necessary
to
raise
pH
and
lower
the
corrosiveness
of
the
product
water.
The
dosages
of
acid,
anti­
scalant,
and
caustic
are
a
function
of
the
feed
water
quality.
Based
on
conversations
with
manufacturers
and
experience
with
similar
NF
systems,
a
typical
cost
for
all
three
chemicals
is
$
0.04
per
1,000
gallons
of
water
produced
for
average
flows
less
than
0.35
mgd,
and
$
0.03
per
1,000
gallons
for
average
flows
above
0.35
mgd.
Therefore,
acid,
anti­
scalant,
and
caustic
chemical
costs
can
be
estimated
by
the
following
equations:

For
average
flows
less
than
0.35
mgd
Acid,
Anti­
Scalant,
and
Caustic
Chemicals
($/
yr)
=
0.04
×
Average
Flow
(
mgd)
×
1,000
×
365
For
average
flows
above
0.35
mgd
Acid,
Anti­
Scalant,
and
Caustic
Chemicals
($/
yr)
=
0.03
×
Average
Flow
(
mgd)
×
1,000
×
365
A
minimum
cost
of
$
50
was
assumed
for
acid/
anti­
scalants
and
caustic
to
account
for
purchasing
these
chemicals
in
small
quantities
of
five
gallons.

NF
Membrane
Replacement
NF
membranes
were
assumed
to
have
a
life
of
five
years,
which
is
typical
for
this
type
of
membrane.
Therefore,
the
annual
cost
for
NF
membrane
replacement
was
assumed
to
be
20
percent
of
the
NF
membrane
purchase
cost.

NF
Membrane
Replacement
($/
yr)
=
0.20
×
NF
Membrane
Element
Process
Cost
Cartridge
Filter
Replacement
Cartridge
filters
collect
particles
and
keep
them
from
depositing
on
to
the
NF
membranes.
These
cartridge
filters
must
be
replaced
more
frequently
for
turbid
waters.
Cost
for
cartridge
filter
replacement
was
assumed
to
be
$
0.002
per
1,000
gallons
of
water
produced
for
systems
with
average
flows
less
than
0.35
mgd
and
$
0.02
per
1,000
gallons
produced
for
systems
with
flows
above
0.35
mgd.
Costs
were
obtained
from
a
study
of
Florida
NF
plants
(
Bergman
1996).

For
average
flows
less
than
0.35
mgd
Cartridge
Filter
Replacement
Cost
($/
yr)
=
0.0002
×
Average
Flow
(
mgd)
×
1,000
×
365
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
109
For
average
flows
above
0.35
mgd
Cartridge
Filter
Replacement
Cost
($/
yr)
=
0.02
×
Average
Flow
(
mgd)
×
1,000
×
365
Repair,
Maintenance
and
Replacement
NF
systems
require
periodic
maintenance
and
repair.
The
O&
M
costs
for
repair,
maintenance,
and
purchase
of
replacement
parts
is
typically
about
$
0.01
per
1,000
gallons
produced
(
Bergman
1996)
for
existing
systems.
A
minimum
cost
of
$
100
per
year
was
assumed
for
repair
and
replacement
for
small
systems.
The
cost
equation
for
repair,
maintenance,
and
replacement
is:

Repair,
Maintenance
&
Replacement
Cost
($/
yr)
=
0.01
*
Average
Flow
(
mgd)
×
1,000
×
365
Performance
Monitoring
In
addition
to
on­
line
conductivity,
pH,
and
turbidity
meters
(
included
in
capital
cost
estimates),
periodic
HPC
tests
are
typically
performed
to
monitor
biological
activity
on
the
finished
water
side
of
the
membrane.
Field
HPC
tests
cost
approximately
$
1
per
test
and
require
one
hour
of
labor.
Thus,
the
cost
per
test,
including
labor
(
at
$
24.96
per
hour),
is
$
25.96.
The
frequency
of
HPC
testing
was
assumed
to
be
one
test
per
membrane
skid
per
week.
As
mentioned
earlier,
the
NF
skid
size
of
2
mgd
was
assumed
for
all
system
sizes.

Power
Power
costs
include
power
for
NF
feed
pumps,
instrumentation
and
controls,
and
building
maintenance.
The
power
requirements
for
process
pumping
and
building
maintenance
were
assumed
to
be
1.2
kWh/
1,000
gallons
and
0.6
kWh/
1,000
gallons,
respectively.
Additional
power
for
instruments
and
controls
was
assumed
to
be
negligible.
Unit
power
cost
of
$
0.076
per
kWh
was
used
to
estimate
the
power
cost.
The
equation
for
power
cost
is
given
below.

Power
Cost
($/
yr)
=
1.8
x
0.076
x
Average
Flow
(
mgd)
x
1,000
x
365
Labor
Technical
labor
estimates
for
operation
and
maintenance
of
the
membrane
systems
include
periodic
data
logging,
repair
of
process
equipment,
and
sampling.
Hours
are
based
on
experience
with
similar
systems.
Consistent
with
other
technologies,
a
technical
labor
rate
of
$
24.96
per
hour
was
assumed.
No
additional
managerial
labor
was
assumed.
A
summary
of
labor
hour
assumptions
is
provided
in
Exhibit
4.53.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
110
Exhibit
4.53:
Summary
of
NF
Technical
Labor
Assumptions
System
Size
(
mgd)
Technical
Labor
(
hrs/
week)

<
0.1
4
0.1
­
1
12
1
­
5
24
5
­
10
40
10
­
100
80
>
100
160
POTW
Surcharge
A
fee
of
$
0.00183
per
1,000
gallons
discharged
to
the
sanitary
sewer
was
assumed.
This
rate
was
based
upon
data
provided
in
the
DPRA
reports
(
1993a
and
1993b).
The
discharge
volume
was
based
on
an
average
system
recovery
of
85
percent;
therefore,
the
waste
volume
is
0.15
×
average
daily
flow.
The
surcharge
for
brine
discharge
can
be
calculated
using
the
equation
below.

Surcharge
for
Brine
Discharge
($/
yr)
=
0.00183
×
0.15
×
Average
Flow
(
mgd)
×
1,000
×
365
Costs
for
concentrate
handling
included
the
following
components:

°
Direct
discharge
of
15
percent
of
the
feed
flow
to
a
sewer/
storm/
salinity
interceptor
or
ocean
outfall,
located
500
feet
or
less
from
the
NF
plant
(
at
85
percent
recovery,
15
percent
would
be
the
brine
stream).

°
No
additional
pumping
is
necessary,
assuming
that
the
brine
stream
is
leaving
the
NF
system
at
30
psi
residual
pressure.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
111
Design
Flow,
mgd
0.007
0.022
0.037
0.091
0.18
0.27
0.36
0.68
1
Average
Flow,
mgd
0.0015
0.0054
0.0095
0.025
0.054
0.084
0.11
0.23
0.35
Unit
Capital
Cost
Summary
Total
Unit
Capital
Cost
$
57,525
$
74,149
$
90,772
$
157,393
$
221,934
$
311,361
$
351,040
$
645,274
$
889,719
Indirect
Capital
Costs
$
9,358
$
9,684
$
10,010
$
11,441
$
27,089
$
35,029
$
42,112
$
69,474
$
137,870
Piloting
$
1,000
$
1,000
$
1,000
$
1,000
$
10,000
$
10,000
$
10,000
$
10,000
$
60,000
Permitting
$
2,500
$
2,500
$
2,500
$
2,622
$
3,500
$
4,964
$
5,550
$
10,344
$
13,506
Land
$
963
$
1,289
$
1,615
$
2,919
$
3,897
$
5,527
$
6,179
$
11,516
$
7,518
Operator
Training
$
0
$
0
$
0
$
0
$
0
$
0
$
1,000
$
1,000
$
3,000
Housing
$
4,895
$
4,895
$
4,895
$
4,900
$
9,692
$
14,538
$
19,384
$
36,615
$
53,845
Capital
Cost
After
Multiplier
$
48,167
$
64,464
$
80,762
$
145,952
$
194,845
$
276,332
$
308,927
$
575,800
$
751,849
Subtotal
Process
Cost
$
28,842
$
38,601
$
48,360
$
87,396
$
116,673
$
165,468
$
184,986
$
344,790
$
450,209
Subtotal
NF
Equipment
Cost
$
19,815
$
29,723
$
39,630
$
79,261
$
108,984
$
158,522
$
178,337
$
340,574
$
445,843
Pipes
and
Valves
$
1,982
$
2,972
$
3,963
$
7,926
$
10,898
$
15,852
$
17,834
$
34,057
$
44,584
Instrumentation
and
Controls
$
3,963
$
5,945
$
7,926
$
15,852
$
21,797
$
31,704
$
35,667
$
68,115
$
89,169
Cartridge
Prefiltration
$
1,585
$
2,378
$
3,170
$
6,341
$
8,719
$
12,682
$
14,267
$
27,246
$
35,667
Acid
and
Anti­
Scalent
Feed
Systems
$
594
$
892
$
1,189
$
2,378
$
3,270
$
4,756
$
5,350
$
10,217
$
13,375
System
Feed
Pumps
$
2,477
$
3,715
$
4,954
$
9,908
$
13,623
$
19,815
$
22,292
$
42,572
$
55,730
Nanofilter
Membrane
Elements
$
3,963
$
5,945
$
7,926
$
15,852
$
21,797
$
31,704
$
35,667
$
68,115
$
89,169
Membrane
Skid
with
Filter
Housing
$
3,963
$
5,945
$
7,926
$
15,852
$
21,797
$
31,704
$
35,667
$
68,115
$
89,169
Clean­
In­
Place
(
CIP)
System
$
991
$
1,486
$
1,982
$
3,963
$
5,449
$
7,926
$
8,917
$
17,029
$
22,292
Online
Conductivity/
pH
and
Turbidity
Meters
$
4,954
$
4,954
$
4,954
$
4,954
$
4,954
$
4,954
$
4,954
$
4,954
$
4,954
500
ft
Brine
Pipeline
Cost
$
4,371
$
4,371
$
4,371
$
4,371
$
4,371
$
4,371
$
4,371
$
4,371
$
6,100
Brine
Discharge
Pump
(
Not
Included)
$
248
$
372
$
495
$
991
$
1,362
$
1,982
$
2,229
$
4,257
$
5,573
Annual
O&
M
Summary
Total
Annual
O&
M
Cost
$
7,789
$
8,800
$
9,872
$
14,051
$
30,613
$
37,777
$
43,061
$
70,281
$
111,819
Acid,
Anti­
Scalant,
Caustic
Chemicals
$
50
$
79
$
139
$
365
$
788
$
1,226
$
1,606
$
3,358
$
3,832
Clean­
in­
Place
Chemicals
$
50
$
50
$
50
$
91
$
197
$
307
$
401
$
839
$
1,277
NF
Membrane
Replacement
$
793
$
1,189
$
1,585
$
3,170
$
4,359
$
6,341
$
7,133
$
13,623
$
17,834
Cartridge
Filter
Replacement
$
30
$
30
$
30
$
30
$
39
$
61
$
80
$
168
$
2,555
Repair,
Maintenance
and
Replacement
$
100
$
100
$
100
$
100
$
197
$
307
$
401
$
839
$
1,277
Process
Monitoring
(
HPCs)
$
1,350
$
1,350
$
1,350
$
1,350
$
1,350
$
1,350
$
1,350
$
1,350
$
1,350
Power
$
75
$
270
$
474
$
1,248
$
2,696
$
4,194
$
5,493
$
11,484
$
17,476
Labor
$
5,192
$
5,192
$
5,192
$
5,192
$
15,575
$
15,575
$
15,575
$
15,575
$
31,150
Surcharge
for
Brine
Discharge
(
Sewer/
Storm
Drain/
Brine
Interceptor)
$
150
$
541
$
952
$
2,505
$
5,410
$
8,416
$
11,021
$
23,044
$
35,067
Exhibit
4.54:
Nanofiltration
Cost
Summary
Note:
Assume
temperature
=
10
°
C,
discharge
to
sewer
Source:
Section
4.5.2
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
112
Design
Flow,
mgd
1.2
2
3.5
7
17
22
76
210
430
520
Average
Flow,
mgd
0.41
0.77
1.4
3
7.8
11
38
120
270
350
Unit
Capital
Cost
Summary
Total
Unit
Capital
Cost
$
1,051,390
$
1,954,756
$
3,286,990
$
6,499,205
$
14,869,801
$
19,105,695
$
55,387,959
$
124,824,207
$
255,424,078
$
306,978,901
Indirect
Capital
Costs
$
152,744
$
214,204
$
325,495
$
587,703
$
1,094,442
$
1,393,455
$
4,189,174
$
10,408,628
$
20,702,259
$
24,903,975
Piloting
$
60,000
$
60,000
$
60,000
$
60,000
$
60,000
$
60,000
$
60,000
$
60,000
$
60,000
$
60,000
Permitting
$
16,143
$
26,108
$
44,422
$
88,673
$
206,630
$
265,684
$
500,000
$
500,000
$
500,000
$
500,000
Land
$
8,986
$
17,406
$
29,615
$
59,115
$
68,877
$
88,561
$
255,994
$
572,078
$
1,173,609
$
1,410,375
Operator
Training
$
3,000
$
3,000
$
3,000
$
3,000
$
10,000
$
10,000
$
25,000
$
25,000
$
25,000
$
25,000
Housing
$
64,614
$
107,690
$
188,458
$
376,915
$
748,935
$
969,210
$
3,348,180
$
9,251,550
$
18,943,650
$
22,908,600
Capital
Cost
After
Multiplier
$
898,646
$
1,740,553
$
2,961,495
$
5,911,502
$
13,775,358
$
17,712,241
$
51,198,785
$
114,415,579
$
234,721,819
$
282,074,926
Subtotal
Process
Cost
$
538,111
$
870,276
$
1,480,748
$
2,955,751
$
6,887,679
$
8,856,120
$
25,599,393
$
57,207,790
$
117,360,910
$
141,037,463
Subtotal
NF
Equipment
Cost
$
535,011
$
866,916
$
1,486,142
$
2,972,284
$
6,935,330
$
8,916,853
$
25,759,798
$
57,464,166
$
117,900,616
$
141,678,891
Pipes
and
Valves
$
53,501
$
86,692
$
148,614
$
297,228
$
693,533
$
891,685
$
2,575,980
$
5,746,417
$
11,790,062
$
14,167,889
Instrumentation
and
Controls
$
107,002
$
173,383
$
297,228
$
594,457
$
1,387,066
$
1,783,371
$
5,151,960
$
11,492,833
$
23,580,123
$
28,335,778
Cartridge
Prefiltration
$
42,801
$
69,353
$
118,891
$
237,783
$
554,826
$
713,348
$
2,060,784
$
4,597,133
$
9,432,049
$
11,334,311
Acid
and
Anti­
Scalent
Feed
Systems
$
16,050
$
26,007
$
44,584
$
89,169
$
208,060
$
267,506
$
772,794
$
1,723,925
$
3,537,018
$
4,250,367
System
Feed
Pumps
$
66,876
$
108,365
$
185,768
$
371,536
$
866,916
$
1,114,607
$
3,219,975
$
7,183,021
$
14,737,577
$
17,709,861
Nanofilter
Membrane
Elements
$
107,002
$
173,383
$
297,228
$
594,457
$
1,387,066
$
1,783,371
$
5,151,960
$
11,492,833
$
23,580,123
$
28,335,778
Membrane
Skid
with
Filter
Housing
$
107,002
$
173,383
$
297,228
$
594,457
$
1,387,066
$
1,783,371
$
5,151,960
$
11,492,833
$
23,580,123
$
28,335,778
Clean­
In­
Place
(
CIP)
System
$
26,751
$
43,346
$
74,307
$
148,614
$
346,767
$
445,843
$
1,287,990
$
2,873,208
$
5,895,031
$
7,083,945
Online
Conductivity/
pH
and
Turbidity
Meters
$
4,954
$
9,908
$
9,908
$
19,815
$
44,584
$
59,446
$
193,198
$
525,104
$
1,070,022
$
1,292,944
500
ft
Brine
Pipeline
Cost
$
6,171
$
6,456
$
6,990
$
8,236
$
11,795
$
13,574
$
32,793
$
80,483
$
158,780
$
190,811
Brine
Discharge
Pump
(
Not
Included)
$
6,688
$
10,836
$
18,577
$
37,154
$
86,692
$
111,461
$
321,997
$
718,302
$
1,473,758
$
1,770,986
Annual
O&
M
Summary
Total
Annual
O&
M
Cost
$
125,926
$
203,795
$
339,238
$
703,226
$
1,763,644
$
2,409,108
$
7,862,441
$
23,730,069
$
52,646,948
$
67,712,655
Acid,
Anti­
Scalant,
Caustic
Chemicals
$
4,489
$
8,431
$
15,329
$
32,848
$
85,405
$
120,442
$
416,073
$
1,313,916
$
2,956,311
$
3,832,255
Clean­
in­
Place
Chemicals
$
1,496
$
2,810
$
5,110
$
10,949
$
28,468
$
40,147
$
138,691
$
437,972
$
985,437
$
1,277,418
NF
Membrane
Replacement
$
21,400
$
34,677
$
59,446
$
118,891
$
277,413
$
356,674
$
1,030,392
$
2,298,567
$
4,716,025
$
5,667,156
Cartridge
Filter
Replacement
$
2,993
$
5,621
$
10,219
$
21,899
$
56,936
$
80,295
$
277,382
$
875,944
$
1,970,874
$
2,554,836
Repair,
Maintenance
and
Replacement
$
1,496
$
2,810
$
5,110
$
10,949
$
28,468
$
40,147
$
138,691
$
437,972
$
985,437
$
1,277,418
Process
Monitoring
(
HPCs)
$
1,350
$
2,700
$
2,700
$
5,400
$
12,149
$
16,199
$
52,647
$
143,092
$
291,583
$
352,329
Power
$
20,472
$
38,448
$
69,905
$
149,796
$
389,470
$
549,252
$
1,897,416
$
5,991,840
$
13,481,640
$
17,476,200
Labor
$
31,150
$
31,150
$
31,150
$
51,917
$
103,834
$
103,834
$
103,834
$
207,667
$
207,667
$
207,667
Surcharge
for
Brine
Discharge
(
Sewer/
Storm
Drain/
Brine
Interceptor)
$
41,079
$
77,148
$
140,270
$
300,578
$
781,502
$
1,102,118
$
3,807,315
$
12,023,100
$
27,051,975
$
35,067,375
Exhibit
4.54
(
continued):
Nanofiltration
Cost
Summary
Note:
Assume
temperature
=
10
°
C,
discharge
to
sewer
Source:
Section
4.5.1
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
113
4.6
Annualized
Costs
To
compare
technologies'
cost
to
one
another,
it
is
helpful
to
annualize
the
capital
costs
and
add
them
to
the
O&
M
costs
to
obtain
an
average
annual
expenditure
for
each
technology.
The
annualization
is
done
according
to
the
methodology
described
in
section
4.3.
Expressing
the
annualized
costs
in
cents
per
thousand
gallons
allows
costs
to
be
expressed
in
similar
units
for
all
size
plants
so
economies
of
scale
and
other
factors
can
be
seen.
Exhibit
4.55
shows
the
annualized
cost
for
each
of
the
technologies
discussed
above
for
all
size
ranges.
Costs
are
annualized
using
a
three
percent
discount
rate
over
a
twenty
year
period,
which
is
the
assumed
lifetime
of
the
equipment.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
114
Design
Flow
0.007
0.022
0.037
0.091
0.18
0.27
0.36
0.68
1
Average
Flow
0.0015
0.0054
0.0095
0.025
0.054
0.084
0.11
0.23
0.35
Bag
Filters
222.4
62.4
46.5
18.1
11.7
9.1
9.0
6.5
6.6
Cartridge
Filters
(
filter
loading
30
pgm/
filter)
260.8
73.0
58.6
29.0
22.6
21.9
21.3
17.6
17.1
Convert
to
Chloramines
(
NH4
dose
=
0.55mg/
l)
628.7
174.8
99.5
38.0
18.3
17.9
13.9
6.9
6.2
Convert
to
Chloramines
(
NH4
dose
=
0.15mg/
l)
628.5
174.6
99.3
37.8
18.0
17.7
13.7
6.8
6.1
GAC
(
EBCT
=
10,
360
day
regeneration)
474.2
285.2
194.6
146.1
130.3
89.7
84.4
GAC
(
EBCT
=
20,
90
day
regeneration)
2,113.4
1,099.2
871.1
621.2
325.8
273.4
255.6
204.3
196.2
GAC
(
EBCT
=
20,
240
day
regeneration)
1,647.8
743.2
556.7
368.8
262.0
211.7
195.1
146.3
139.5
Nanofiltration
(
100%
flow
treated,
10C)
2,128.9
699.3
460.6
269.9
231.0
191.5
166.0
135.4
134.3
Chlorine
Dioxide
(
ClO2
dose
=
1.25
mg/
l,
no
additional
contact
time)
186.4
94.2
63.3
49.2
24.7
16.7
Ozone
(
0.5
log
dose,
12
minute
contact
time)
845.5
400.7
276.4
214.6
115.6
80.9
Ozone
(
1.0
log
dose,
12
minute
contact
time)
846.8
423.1
277.2
231.2
120.0
91.6
Ozone
(
2.0
log
dose,
12
minute
contact
time)
894.8
424.2
298.8
240.0
139.6
99.2
UV
(
dose
=
40
mJ/
cm2,
UV254
=
0.05,
turbidity
=
0.1
NTU,
Alk
=
60
mg/
l,
Hardness
=
100
mg/
l)
742.7
217.1
139.8
68.4
37.5
31.4
26.9
17.4
18.8
UV
(
dose
=
200
mJ/
cm2,
UV254
=
0.05,
turbidity
=
0.1
NTU,
Alk
=
60
mg/
l,
Hardness
=
100
mg/
l)
972.4
290.8
189.6
97.0
59.4
48.9
42.4
29.1
32.6
UV
with
UPS
(
dose
=
40
mJ/
cm2,
UV254
=
0.05,
turbidity
=
0.1
NTU,
Alk
=
60
mg/
l,
Hardness
=
100
mg/
l)
754.5
220.3
142.5
70.1
38.9
33.0
28.5
19.1
20.5
UV
with
UPS
(
dose
=
200
mJ/
cm2,
UV254
=
0.05,
turbidity
=
0.1
NTU,
Alk
=
60
mg/
l,
Hardness
=
100
mg/
l)
1,252.4
427.3
289.0
145.0
80.6
70.3
67.4
42.1
49.1
Microfiltration/
Ultrafiltration
(
T
=
10C,
sewer
discharge)
2,860.9
1,088.6
737.1
397.4
324.6
244.4
210.4
136.9
135.1
Ozone
w/
pH
adj
(
0.5
log
dose,
12
minute
contact
time)
873.1
426.3
297.1
233.3
130.6
94.8
Ozone
w/
pH
adj
(
1.0
log
dose,
12
minute
contact
time)
874.4
448.7
297.9
249.8
135.0
105.5
Ozone
w/
pH
adj
(
2.0
log
dose,
12
minute
contact
time)
922.4
449.8
319.5
258.6
154.7
113.1
Combined
Filter
Performance
61.8
41.5
In
Bank
Filtration
Secondary
Filters
Watershed
Control
Presedimentation
Basins
Data
Not
Used
Data
Not
Used
Data
Not
Used
Exhibit
4.55:
Annualized
Cost
Summary
Source:
Derived
from
sections
4.4
and
4.5
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
4­
115
Design
Flow
1.2
2
3.5
7
17
22
76
210
430
520
Average
Flow
0.41
0.77
1.4
3
7.8
11
38
120
270
350
Bag
Filters
6.6
6.2
Cartridge
Filters
(
filter
loading
30
pgm/
filter)
18.2
16.4
Convert
to
Chloramines
(
NH4
dose
=
0.55mg/
l)
7.7
4.3
2.6
1.4
0.8
0.7
0.4
0.3
0.2
0.2
Convert
to
Chloramines
(
NH4
dose
=
0.15mg/
l)
7.5
4.1
2.4
1.3
0.6
0.5
0.2
0.1
0.1
0.1
GAC
(
EBCT
=
10,
360
day
regeneration)
77.9
53.7
40.7
30.0
21.8
18.8
13.6
10.0
8.4
7.9
GAC
(
EBCT
=
20,
90
day
regeneration)
185.6
121.5
87.5
61.8
46.4
41.5
32.2
25.1
21.5
20.3
GAC
(
EBCT
=
20,
240
day
regeneration)
123.1
83.6
62.6
45.9
34.2
30.1
23.0
17.7
14.9
13.8
Nanofiltration
(
100%
flow
treated,
10C)
131.4
119.3
109.6
104.1
97.1
92.0
83.5
73.3
70.8
69.2
Chlorine
Dioxide
(
ClO2
dose
=
1.25
mg/
l,
no
additional
contact
time)
16.3
9.6
6.6
3.5
1.8
1.5
0.9
0.6
0.5
0.5
Ozone
(
0.5
log
dose,
12
minute
contact
time)
73.7
49.1
32.3
20.3
12.9
10.6
8.3
6.2
5.0
4.8
Ozone
(
1.0
log
dose,
12
minute
contact
time)
85.9
52.2
35.4
24.4
14.2
12.2
9.9
7.3
6.4
6.0
Ozone
(
2.0
log
dose,
12
minute
contact
time)
91.3
56.4
38.3
32.2
21.2
18.6
15.7
12.2
10.9
10.2
UV
(
dose
=
40
mJ/
cm2,
UV254
=
0.05,
turbidity
=
0.1
NTU,
Alk
=
60
mg/
l,
Hardness
=
100
mg/
l)
16.8
11.4
8.1
5.5
3.9
3.4
2.7
2.3
2.1
2.0
UV
(
dose
=
200
mJ/
cm2,
UV254
=
0.05,
turbidity
=
0.1
NTU,
Alk
=
60
mg/
l,
Hardness
=
100
mg/
l)
30.3
22.1
16.9
13.5
11.5
10.3
9.0
8.0
7.4
7.1
UV
with
UPS
(
dose
=
40
mJ/
cm2,
UV254
=
0.05,
turbidity
=
0.1
NTU,
Alk
=
60
mg/
l,
Hardness
=
100
mg/
l)
18.5
13.3
9.3
6.4
4.6
3.9
3.1
2.5
2.3
2.2
UV
with
UPS
(
dose
=
200
mJ/
cm2,
UV254
=
0.05,
turbidity
=
0.1
NTU,
Alk
=
60
mg/
l,
Hardness
=
100
mg/
l)
50.5
35.2
33.4
23.4
23.5
39.2
27.4
18.0
8.3
9.2
Microfiltration/
Ultrafiltration
(
T
=
10C,
sewer
discharge)
125.6
100.4
84.2
73.0
63.7
57.9
52.2
45.1
41.0
38.9
Ozone
w/
pH
adj
(
0.5
log
dose,
12
minute
contact
time)
87.3
61.7
44.5
32.1
24.5
22.2
19.9
17.6
16.4
16.1
Ozone
w/
pH
adj
(
1.0
log
dose,
12
minute
contact
time)
99.5
64.9
47.7
36.3
25.9
23.8
21.5
18.8
17.8
17.4
Ozone
w/
pH
adj
(
2.0
log
dose,
12
minute
contact
time)
105.0
69.1
50.5
44.1
32.9
30.2
27.3
23.7
22.3
21.6
Combined
Filter
Performance
14.9
6.9
6.2
2.7
0.0
In
Bank
Filtration
4.6
4.6
4.6
Secondary
Filters
62.4
22.0
8.9
Watershed
Control
115.3
43.6
12.8
Presedimentation
Basins
49.6
15.5
11.3
Data
Not
Used
Exhibit
4.55
(
continued):
Annualized
Cost
Summary
Source:
Derived
from
sections
4.4
and
4.5
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
1
5.
References
Adham,
Samer
S.,
Snoeyink,
V.
J.,
Clark,
M.
M.
and
C.
Anselme.
1993.
"
Predicting
and
Verifying
Organics
Removal
by
PAC
in
Pilot­
scale
UF
Systems."
J.
AWWA,
85:
12:
58.

Adham,
Samer
S.,
Snoeyink,
V.
J.,
Clark,
M.
M.
and
Bersillon,
Jean­
Luc.
1991.
"
Predicting
and
Verifying
Organics
Removal
by
PAC
in
an
Ultrafiltration
System."
J.
AWWA,
83:
12:
81.

Allgeier,
S.
A.
and
R.
S.
Summers.
1995.
"
Evaluating
Nanofiltration
for
DBP
Control
with
the
RBSMT,"
J.
AWWA,
86:
3:
87­
99.

Amy,
G.
L.
and
M.
S.
Siddiqui.
1999.
Strategies
to
Control
Bromate
and
Bromide.
Report
No.
90751,
AWWARF,
Denver,
CO.

Anselme,
C.
and
Charles,
P.
1990.
"
The
Use
of
Powdered
Activated
Carbon
for
the
Removal
of
Specific
Pollutants
in
Ultrafiltration
processes."
Laboratoire
Central,
Lyonnaise
des
Eaux,
Le
Pecq,
France.

APHA­
AWWA­
WEF.
1998.
Standard
methods
for
the
examination
of
water
and
wastewater,
20th
ed.
Washington,
DC.

Arora,
H.,
M.
W.
LeChevallier,
and
K.
L.
Dixon.
1997.
"
DBP
Occurrence
Survey."
J.
AWWA,
89:
6:
60­
68.

AWWA.
1969.
Water
Treatment
Plant
Design.
First
Edition,
American
Water
Works
Association,
Inc.

AWWA.
1999.
Water
Quality
and
Treatment.
Fifth
Edition,
McGraw­
Hill,
New
York,
NY.

AWWA
and
ASCE.
1998.
Water
Treatment
Plant
Design.
Third
Edition,
McGraw­
Hill,
New
York,
NY.

AWWSC.
1998.
Evaluation
of
Chlorine
Dioxide
for
Inactivation
of
Cryptosporidium
and
Byproduct
Control.
AWWSC,
Voorhees,
NJ.

Babcock,
D.
B.
and
Singer,
P.
C.
1979.
"
Chlorination
and
Coagulation
of
Humic
and
Fulvic
Acids."
J.
AWWA,
71:
3:
149.

Battigelli,
D.
A.,
M.
D.
Sobsey
and
D.
C.
Lobe.
1993.
"
The
Inactivation
of
Hepatitis
A
Virus
and
Other
Model
Viruses
by
UV
Irradiation."
Wat.
Sci.
Tech.,
27:
3­
4:
339­
342.

Benedek,
A.,
Bancsi,
J.
J.,
Malaiyandi,
M.
and
Lancaster,
E.
A.
1979.
"
The
Effect
of
Ozone
on
the
Biological
Degradation
and
Activated
Carbon
Adsorption
of
Natural
and
Synthetic
Organics
in
Water.
Part
II.
Adsorption."
Ozone
Sci.
Eng.,
1:
4:
347.

Bergman
R.
A.
1996.
"
Cost
of
Membrane
Softening
in
Florida",
J.
AWWA,
88:
5:
32.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
2
Bolton,
J.
R.
1999.
Ultraviolet
Applications
Handbook.
Bolton
Photosciences,
Inc.,
Ayr,
Ontario,
Canada.

Bouwer,
E.
J.
and
Crowe,
P.
B.
1988.
"
Biological
Processes
in
Drinking
Water
Treatment."
J.
AWWA,
80:
9:
82.

Bukhari,
Z.;
Hargy,
T.
H.;
Bolton,
J.
R.,
Dussert
B.,
and
Clancy
J.
L.
1998.
"
Inactivation
of
Cryptosporidium
Parvum
Oocysts
Using
Medium­
Pressure
Ultraviolet
Light."
Proceedings,
1998
Annual
AWWA
Conference,
Dallas,
TX.

Bukhari,
Z.,
T.
M.
Hargy,
J.
R.
Bolton,
B.
Dussert
and
J.
L.
Clancy.
1999)
"
Medium­
Pressure
UV
Light
for
Oocyst
Inactivation."
J.
AWWA,
91:
3:
86­
94.

Cairns,
B.
1999.
"
Ultraviolet
Water
Disinfection."
USEPA
Workshop
on
UV
Disinfection
of
Drinking
Water,
April
28­
29,
1999,
Arlington,
VA.

Camel,
V.,
and
Bermond,
A.
1999.
"
The
Use
of
Ozone
and
Associated
Oxidation
Processes
in
Drinking
Water
Treatment."
Water
Research,
32:
11:
3208­
3222.

Campbell,
A.
T.
2000.
""
In
press.

Campbell,
A.
T.,
Robertson,
L.
J.,
and
Smith,
H.
V.
1995b.
"
Inactivation
of
Oocysts
of
Cryptosporidium
parvum
by
Ultraviolet
Irradiation."
Wat.
Res.,
29:
2583.

Campbell,
S.,
B.
W.
Lykins,
J.
A.
Goodrich,
D.
Post
and
T.
Lay.
1995a.
"
Package
Plants
for
Small
Systems:
A
Field
Study."
J.
AWWA,
87:
11:
39­
47.

Carlson,
M.
and
D.
Hardy.
1998.
"
Controlling
DBPs
with
Monochloramine."
J.
AWWA,
90:
2:
95­
105.

CH2M
Hill.
1986.
Pilot
Plant
Report
for
Department
of
Public
Utilities,
Newport
News,
Virginia.
Vol.
1,
Newport
News,
VA.

Chadik,
P.
A.
and
Amy,
G.
L.
1983.
"
Removing
Trihalomethane
Precursors
from
Various
Natural
Waters
by
Metal
Coagulants."
J.
AWWA,
75:
10:
532.

Chadik,
P.
A.
and
Amy,
G.
L.
1987.
"
Molecular
Weight
Effects
of
THM
Control
by
Coagulation
and
Adsorption."
J.
Env.
Eng.,
113:
6:
1234.

Chang,
J.
C.
H.,
S.
F.
Osoff,
D.
C.
Lobe,
M.
H.
Dorfman,
C.
M.
Dumais,
R.
G.
and
J.
D.
Johnson.
1985.
"
UV
Inactivation
of
Pathogenic
and
Indicator
Organisms."
Applied
and
Environmental
Microbiology,
49:
6:
1361.

Chang,
S.
D.
and
Singer,
P.
C.
1991.
"
The
Impact
of
Ozonation
on
Particle
Stability
And
The
Removal
of
TOC
And
THM
Procursors."
J.
AWWA,
83:
3:
71.

Chellam,
S.,
Jacangelo,
J.,
Bonacquisti,
T.,
Schauer,
B.
1997.
"
Effect
of
Pretreatment
on
Surface
Water
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
3
Nanofiltration."
J.
AWWA,
89:
10:
77.

Chen,
A.
S.
C.,
V.
L.
Snoeyink
and
F.
Fiessinger.
1987.
"
Activated
Alumina
Adsorption
of
Dissolved
Organic
Compounds
Before
and
After
Ozonation."
Environ.
Sci.
Technol.,
21:
1:
83.

Cho,
J,
Amy,
G.,
Pellgrino,
J.
1999.
"
Membrane
Filtration
of
Natural
Organic
Matter:
Initial
Comparison
of
Rejection
and
Flux
Decline
Characteristics
with
Ultrafiltration
and
Nanofiltration
Membranes."
Water
Resources,
33:
11:
2517­
2526.

Chowdhury,
Z.
K.,
J.
A.
Roberson
and
D.
M.
Owen.
1997.
"
A
National
Evaluation
of
Enhanced
Coagulation
and
Enhanced
Softening."
AWWA
Annual
Conference
Proceedings,
Atlanta,
GA.

Clair,
D.,
S.
Randtke,
P.
Adams,
and
S.
Shreve.
1997.
"
Microfiltration
of
a
High­
Turbidity
Surface
Water
with
Post­
treatment
by
Nanofiltration
and
Reverse
Osmosis,"
AWWA
Membrane
Technology
Conference
Proceedings,
February
23
­
26,
1997,
New
Orleans,
LA.

Clancy,
J.
1999.
"
Watershed
Monitoring
for
Determining
Variability
of
Giardia
and
Cryptosporidium
Concentrations."
1999
AWWA
Water
Quality
Technology
Conference
Proceedings,
Tampa
Bay,
FL.

Clancy,
J.,
Hargy,
T.,
and
Dyksen,
J.
1998.
UV
Light
Inactivation
of
Cryptosporidium
Oocysts.
J.
AWWA,
90:
9:
92.

Clancy,
J.
L.,
Z.
Bukhari,
T.
M.
Hargy,
J.
R.
Bolton,
B.
W.
Dussert,
and
M.
M.
Marshall.
2000.
"
Using
UV
to
Inactivate
Cryptosporidium."
J.
AWWA,.
92:
9:
97.

Clark
et
al.
1994.
"
DBP
Control
in
Drinking
Water:
Cost
and
Performance."
J.
of
Environmental
Engineering,
120:
4:
759.

Clark,
R.
M.
1987.
"
Modeling
TOC
Removal
by
GAC:
The
General
Logistic
Function."
J.
AWWA,
79:
1:
33.

Clark,
R.
M.,
J.
Q.
Adams,
V.
Sethi
and
M.
Sivaganesan.
1998.
"
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
for
Drinking
Water
in
the
US:
Cost
and
Performance."
Aqua,
47:
6:
255­
265.

Clesceri,
L.
S.,
Greenberg,
A.
E.
and
Trussell,
R.
R.
eds.
1989.
Standard
Methods
for
the
Examination
of
Water
and
Wastewater.
17th
Edition,
AWWA,
WPCF,
APHA.

Collins,
M.
R.,
Amy,
G.
L.
and
King,
P.
H.
1985.
"
Removal
of
Organic
Matter
in
Water
Treatment."
J.
Env.
Eng.,
111(
6),
p.
850.

Colvin,
C.,
C.
Acker,
B.
Marinas,
and
J.
Lozier.
1999.
"
Mechanisms
Responsible
for
the
Passage
of
Microorganisms
through
RO
and
NF
Membranes,"
AWWA
Membrane
Technology
Conference
Proceedings,
February
28
­
March
3,
1999,
Long
Beach,
CA.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
4
Conley,
W.
R.
1961.
"
Experiences
with
Anthracite
Sand
Filters."
J.
AWWA,
53
(
12):
1473.

Conley,
W.
R.,
and
R.
W.
Pitman.
1960.
"
Test
Program
for
Filter
Evaluation
at
Hanford."
J.
AWWA,
52(
2):
205.

Conlon,
W.
J.
and
S.
A.
McClellan.
1989.
"
Membrane
Softening:
A
Treatment
Process
Comes
of
Age,"
J.
AWWA,
81:
11:
47.

Cotton
,
C.
A.,
Linden
,
K.
G.,
Schmelling
,
D.
C.,
Bell
,
C.
F.,
and
Darnault,
C.
2001.
"
The
Development,
Application,
and
Cost
Implications
of
the
UV
Dose
Tables
for
LT2ESWTR
Compliance."
Proceedings,
Water
Quality
Technology
Conference,
Nashville,
TN
November
11­
14,
2001.

Cowman,
G.
A.
and
P.
C.
Singer.
1996.
"
Effect
of
Bromide
Ion
on
Haloacetic
Acid
Speciation
Resulting
from
Chlorination
and
Chlorimination
of
Aquatic
Humic
Substances."
Env.
Sci.
Tech
30(
1):
16­
24.

Crozes,
G.,
Seacord,
T.
1999.
"
Ultrafiltration
to
Meet
Multiple
Treatment
Objectives
in
Lime
Softening
Plants."
AWWA
Membrane
Technology
Conference
Proceedings,
Long
Beach,
CA.

Culp/
Wesner/
Culp.
1979.
Estimating
Water
Treatment
Costs,
Volume
2:
Cost
Curves
Applicable
to
1
to
200
mgd
Treatment
Plants,
CWC
Engineering,
San
Clemente,
CA.

Culp/
Wesner/
Culp.
1984.
Estimation
of
Small
System
Water
Treatment
Costs,
CWC
Engineering
Software,
San
Clemente,
CA.

Culp/
Wesner/
Culp.
1994.
WATERCO$
T
Model
­
A
Computer
Program
for
Estimating
Water
and
Wastewater
Treatment
Costs,
Version
2.0,
CWC
Engineering
Software,
San
Clemente,
CA.

Culp/
Wesner/
Culp.
2000.
WATERCO$
T
Model
­
A
Computer
Program
for
Estimating
Water
and
Wastewater
Treatment
Costs,
Version
3.0,
CWC
Engineering
Software,
San
Clemente,
CA.

Dempsey,
B.
A.,
Ganho,
R.
M.
and
O'Melia,
C.
R.
1984.
"
The
Coagulation
of
Humic
Substances
by
Means
of
Aluminum
Salts."
J.
AWWA,
76:
4:
141.

Dempsey,
B.
A.
and
O'Melia,
C.
R.
1983.
"
The
Protonation
and
Complexation
of
Four
Fulvic
Acid
Fractions."
in
Aquatic
and
Terrestrial
Humic
Materials,
R.
F.
Christman
and
E.
T.
Gjessing
eds.,
Ann
Arbor,
Michigan:
Ann
Arbor
Sciences.

Dominngue,
E.
L.,
et
al.
1988.
"
Effects
of
Three
Oxidizing
Biocides
on
Legionella
Pneumophila
Serogroup
1.
Applied
Environmental
Microbiology,
40:
11­
30.

DPRA.
1993a.
Small
Water
System
Byproducts
Treatment
and
Disposal
Cost
Document,
Prepared
for
USEPA
Office
of
Groundwater
and
Drinking
Water.

DPRA.
1993b.
Water
System
Byproducts
Treatment
and
Disposal
Cost
Document,
Prepared
for
USEPA
Office
of
Groundwater
and
Drinking
Water.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
5
Driedger,
A.
M.,
S.
A.
Rubin,
J.
L.
Rennecker
and
B.
J.
Marinas.
1999.
"
Inactivation
of
Cryptosporidium
parvum
Oocysts
with
Free
Chlorine
and
Monochloramine
in
Single­
step
and
Sequential
Disinfection
Schemes."
1999
AWWA
Annual
Conference
Proceedings,
Chicago,
IL.

Driedger,
A.
M.,
S.
A.
Rubin,
J.
L.
Rennecker
and
B.
J.
Marinas.
2000.
"
Sequential
Inactivation
of
Cryptosporidium
parvum
Oocysts
with
Ozone
and
Free
Chlorine."
Wat.
Res.
34:
14:
3591­
3597.

Dryfuse,
M.
J.,
Miltner
R.
J.,
Summers,
R.
S.
1995.
"
The
Removal
of
Molecular
Size
and
Humic/
Nonhumic
Fractions
of
DBP
Precursors
by
Optimized
Coagulation."
Amer.
Water
Works
Assoc.
Annual
Conference
Proceedings,
Anaheim,
CA.

Dugan,
N.
R.,
Fox,
K.
R.,
Owens,
J.
H.,
and
R.
J.
Miltner.
2001.
"
Controlling
Cryptosporidium
Oocysts
Using
Conventional
Treatment."
J.
AWWA
93.12:
64­
76.

Dugan,
N.
R.,
K.
R.
Fox,
R.
J.
Miltner,
D.
A.
Lytle,
D.
J.
Williams,
C.
J.
Parrett,
C.
M.
Feld,
and
J.
H.
Owens.
1999.
"
Control
of
Cryptosporidium
oocysts
by
steady­
state
conventional
treatment."
EPA
Water
Supply
and
Water
Resources
Division,
Cincinnati.
Annual
Conference
Proceedings
of
the
American
Water
Works
Association.
#
ACE99567.

Duguet,
J.
P.,
Dussert,
B.,
Mallevialle,
J.
and
Fiessinger,
F.
1987.
"
Polymerization
Effects
of
Ozone:
Applications
to
the
Removal
of
Phenolic
Compounds
From
Industrial
Wastewaters."
Water
Sci.
Tech.,
19:
919.

Dulin,
B.
E.
and
Knocke,
W.
R.
1989.
"
The
Impact
of
Incorporated
Organic
Matter
on
the
Dewatering
Characteristics
of
Aluminum
Hydroxide
Sludges."
J.
AWWA,
81:
5:
74.

Duranceau,
S.,
Thorner,
K.,
McAleese,
P.
1998.
"
The
Olivenhain
Water
Supply
Project
and
Integrated
Membrane
Systems."
Microfiltration
II
Conference
of
the
National
Water
Research
Institute
Proceedings,
San
Diego,
CA.

Edwards,
M.
1997.
"
Predicting
DOC
Removal
during
Enhanced
Coagulation."
J.
AWWA,
89:
5:
78.

Edwards,
M.,
M.
Boller.,
M.
M.
Benjamin.
1993.
"
Effect
of
Pre­
Ozonation
on
Removal
of
Organic
Matter
during
Water
Treatment
Plant
Operations."
Water
Science
Technology,
27:
ll:
37­
45.

Edzwald,
J.
K.
1984.
Removal
of
Trihalomethane
Precursors
by
Direct
Filtration
and
Conventional
Treatment.
USEPA
Municipal
Environmental
Research
Laboratory,
Cincinnati,
OH.
Rpt.
No.
EPA/
600/
2­
84/
068,
NTIS
Publ.
No.
PB84­
163278.

Edzwald,
J.
K.
1990.
"
Aluminum
Coagulation
of
Natural
Organic
Matter,"
4th
International
Guthenburg
Symposium
on
Chemical
Treatment
Proceedings,
Madrid,
Spain.

El­
Rehaili,
A.
M.
and
Weber,
W.
J.
1987.
"
Correlation
of
Humic
Substance
Trihalomethane
Formation
Potential
and
Adsorption
Behavior
to
Molecular
Weight
Distribution
in
Raw
and
Chemically
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
6
Emelko,
M.
B.,
Huck
P.
M,
Douglas,
I.
P,
and
J.
Van
Den
Oever.
2000.
"
Cryptosporidium
and
Microsphere
Removal
During
Low
Turbidity
End­
Of­
Run
and
Early
Breakthrough
Filtration."
Proceedings
from
AWWA
Water
Quality
Technology
Conference.
Treated
Waters."
Water
Research.,
21:
5:
573.

Emelko,
M.
B.,
Huck,
P.
M.,
and
R.
M.
Slawson.
1999.
"
Design
and
Operational
Strategies
for
Optimizing
Cryptosporidium
Removal
by
Filters."
Conference
proceedings
of
the
AWWA
Water
Quality
Technical
Conference.

Escobar,
I.,
Randall,
A.
1999.
"
Influence
of
NF
on
Distribution
Systems
Biostability."
J.
AWWA,
91:
9:
76.
Faust,
S.
D
and
O.
M
Aly.
1999.
Chemistry
of
Water
Treatment,
Second
Edition,
Lewis
Publishers,
CRC
Press,
Boca
Raton,
FL.

Finch,
G.
1999.
"
Inactivation
of
C.
parvum
and
G.
muris
with
Medium
Pressure
Ultraviolet
Radiation."
USEPA
Workshop
on
UV
Disinfection
of
Drinking
Water,
April
28­
29,
1999,
Arlington,
VA.

Finch,
G.
R.
1997.
"
Control
of
Cryptosporidium
Through
Chemical
Disinfection:
Current
State­
of­
the­
Art."
AWWARF
Technology
Transfer
Conference,
Portland,
OR.

Finch,
G.
R.,
Black,
E.
K.,
and
Gyurek,
L.
L.
1994.
"
Ozone
and
Chlorine
Inactivation
of
Cryptosporidium."
WQTC,
San
Francisco,
CA.

Finch,
G.
R.,
L.
R.
J.
Liyanage,
and
M.
Belosevic.
1995.
"
Effects
of
Chlorine
Dioxide
on
Cryptosporidium
and
Giardia."
Third
International
Symposium
on
Chlorine
Dioxide:
Drinking
Water,
Process
Water,
and
Wastewater
Issues
Conference
Proceedings,
AWWA
and
AWWARF,
New
Orleans,
LA.

Fronk,
C.
A.
1987.
"
Destruction
of
Volatile
Organic
Contaminants
in
Drinking
Water
By
Ozone
Treatment."
Ozone
Sci.
Eng.,
9:
265.

Fu,
L.
F.,
Dempsey,
B.
1997.
"
Effects
of
Charge
and
Coagulant
Dose
on
NOM
Removal
and
Membrane
Fouling
Mechanisms."
AWWA
Membrane
Technology
Conference
Proceedings,
New
Orleans,
LA.

Fu,
P.
Ruiz,
H.,
Lozier,
J.,
Thomspon,
K.,
Spangenberg,
C.
1995.
"
A
Pilot
Study
on
Groundwater
Natural
Organics
Removal
by
Low­
Pressure
Membranes."
Desalination,
102:
47­
56.

Gagliardo,
P.,
S.
Adham,
Y.
Chambers,
B.
Gallagher,
M.
Sobsey,
and
R.
Trussel.
1999.
"
Development
of
an
Innovative
Method
to
Monitor
the
Integrity
of
a
Membrane
Water
Repurifiation
System,"
AWWA
Membrane
Technology
Conference
Proceedings,
February
28
­
March
3,
1999,
Long
Beach,
CA.

Gagliardo,
P.,
S.
Adham,
and
R.
Trussel.
1997.
"
Water
Repurification
Using
Reverse
Osmosis:
Thin
Film
Composite
vs.
Cellulose
Acetate
Membranes,"
AWWA
Membrane
Technology
Conference
Proceedings,
February
23
­
26,
1997,
New
Orleans,
LA.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
7
Glaze,
W.
H.
et
al.
1982.
Pilot­
Scale
Evaluation
of
Biological
Activated
Carbon
for
the
Removal
of
THM
Precursors.
USEPA
Municipal
Environmental
Research
Laboratory,
Cincinnati,
OH.
Rpt.
No.
EPA/
600/
S2­
82/
046.

Glaze,
W.
H.,
Peyton,
G.
R.,
Huang,
F.
Y.,
Burleson,
J.
L.
and
Jones,
P.
C.
1980.
Oxidation
of
Water
Supply
Refractory
Species
By
Ozone
With
Ultraviolet
Radiation.
USEPA,
Cincinnati,
OH,
EPA­
600/
2­
80­
110.

Glaze,
W.
H.,
H.
S.
Weinberg,
and
J.
E.
Cavanagh.
1993.
"
Evaluating
the
Formation
of
Brominated
DBPs
During
Ozonation,"
J.
AWWA,
85:
1:
96­
103.

Glucina,
K.,
J­
M.
Laine,
and
C.
Robert.
1997.
"
Integrated
Multi­
Objective
Membrane
Systems
for
Surface
Water
Treatment,"
AWWA
Membrane
Technology
Conference
Proceedings,
February
23
­
26,
1997,
New
Orleans,
LA.

Goodrich,
J.
A,
S.
Y.
Li,
and
B.
W.
Lykins.
1995.
"
Cost
and
Performance
of
Alternative
Filtration
Technologies
for
Small
Communities."
Proceedings
of
the
1995
American
Water
Works
Association
Annual
Conference.

Grasso,
D.
and
Weber,
W.
J.
1988.
"
Ozone
Induced
Particle
Destabilization."
J.
AWWA,
80:
8:
73.

Gurol,
M.
D.
and
Singer,
P.
C.
1983.
"
Dynamics
of
Ozonation
of
Phenol.
I.
Experimental
Observations."
Water
Research,
17(
9):
1173.

Gurol,
M.
D.
and
Singer,
P.
C.
1983.
"
Dynamics
of
Ozonation
of
Phenol.
II.
Mathematical
Simulation."
Water
Research,
17(
9):
1173.

Gyurek,
L.
L.,
Li,
H.,
Belosevic,
M.,
and
Finch,
R,
G.
1999.
"
Ozone
Inactivation
Kinetics
of
Cryptosporidium
in
Phosphate
Buffer."
J.
of
Environmental
Engineering,
125(
10):
913.

Haag,
W.
R.
and
J.
Hoigne
(
1983).
"
Ozonation
of
Bromide
Containing
Waters:
Kinetics
of
Formation
of
Hypobromous
Acid
and
Bromate,"
Environmental
Science
and
Technology,
17:
5:
261.

Hagedorn,
C.,
S.
L.
Robinson,
J.
R.
Filtz,
S.
M.
Grubss,
T.
A.
Angier,
and
R.
B.
Reneau,
Jr.
1999.
"
Determining
sources
of
fecal
pollution
in
a
rural
Virginia
watershed
with
antibiotic
resistance
patterns
in
fecal
streptococci."
Appl.
Env.
Micorbiology,
65(
12):
5522­
31.

Hagen,
K.
1998.
"
Removal
of
Particles,
Bacteria,
and
Parasites
with
Ultrafiltration
for
Drinking
Water
Treatment,"
Desalination,
119:
85­
91.

Hall,
T.
and
B.
Croll.
1996.
"
The
UK
Approach
to
Cryptosporidium
Control
in
Water
Treatment."
Proceedings
AWWA
Water
Quality
Technology
Conference.
Boston:
.

Hall,
T.,
Pressdee,
J.,
and
E.
Carrington
1994.
"
Removal
of
Cryptosporidium
Oocysts
By
Water
Treatment
Processes."
Foundation
for
Water
Research.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
8
Hargy,
T.
M.
2000.
"
UV
Equipment
Proven
Against
Cryptosporidium."
Water
Conditioning
and
Purification.
March,
p.
36­
38.

Harrington,
G.
W.
and
DiGiano,
F.
A.
1989.
"
Adsorption
Equilibria
of
Natural
Organic
Matter
After
Ozonation."
J.
AWWA,
81:
6:
93.

Havelaar,
A.
H.,
M.
van
Olphen,
and
J.
F.
Schijven.
1995.
"
Removal
and
inactivation
of
viruses
by
drinking
water
treatment
processes
under
full­
scale
conditions."
Wat.
Sci.
Technol.,
31:
55062.

Heneghan,
K.
and
Clark,
M.
1991.
"
Surface
Water
Treatment
by
Combined
Ultrafiltration/
PAC
Adsorption/
Coagulation
for
Removal
of
Natural
Organics,
Turbidity,
and
Bacteria.
AWWA
Membrane
Technology
Conference
Proceedings,
Orlando,
FL.

Hofman,
J.
A.,
M.
M.
Beumer,
E.
T.
Baars,
J.
P.
van
der
Hoek
and
H.
M.
M.
Kopers.
1998.
"
Enhanced
Surface
Water
Treatment
by
Ultrafiltration,"
Desalination,
119:
113­
125.

Hoigne
J.,
and
H.
Bader.
1976.
Role
of
Hydroxyl
Radical
Reactions
in
Ozonation
Processes
in
Aqueous
Solutions,
Water
Res.
10:
377.

Hooper,
S.
M.,
Summers
R.
S.,
Hong
S.
1996b.
"
A
Systematic
Evaluation
of
the
Role
of
Influent
TOC
and
pH
on
GAC
Performance
After
Enhanced
Coagulation."
American
Water
Works
Assoc.
Water
Quality
Technology
Conference
Proceedings,
Boston,
MA.

Hooper,
S.
M.,
Summers
R.
S.,
Solarik
G.,
Hong
S.
1996a.
"
GAC
Performance
for
DBP
Control:
Effect
of
Influent
Concentration,
Seasonal
Variation,
and
Pretreatment."
AWWA
Conference
Proceedings,
Toronto,
Canada.

Hooper,
S.
M.,
Summers
R.
S.,
Solarik
G.,
Owen
D.
M.
1996c.
"
Improving
GAC
Performance
by
Optimized
Coagulation."
J.
AWWA,
88:
8:
107­
120.

Hubel,
R.
E.
and
Edzwald,
J.
K.
1987.
"
Removing
Trihalomethane
Precursors
by
Coagulation."
J.
AWWA,
79:
7:
98.

Huber,
C.
1984.
Adsorption
and
Biologischer
Abbau
van
Huminstoffen
in
Activkohlfiltern.
Dissertation
(
in
German),
Univ.
Karlsruhe,
West
Germany.

Huck,
P.
M.,
Anderson,
W.
B.,
Rowley,
S.
M.
and
Daignault,
S.
A.
1990.
"
Formation
and
Removal
of
Selected
Aldehydes
in
a
Biological
Drinking
Water
Treatment
Process."
Presented
at
the
1990
Spring
Conference
of
the
International
Ozone
Association,
Shreveport,
LA.

Huey,
B.,
Heckler,
J.,
Joost,
R.,
Crozes,
G.,
Gallier,
T.
1999.
"
Combination
of
Powdered
Activated
Carbon
and
Low
Pressure
Membrane
Filtration:
A
Process
Alternative
for
SRP
Water
Treatment."
AWWA
Membrane
Technology
Conference
Proceedings,
Long
Beach,
CA.

Jacangelo,
J.
G.,
S.
Adham,
J­
M.
Laine.
1997.
Membrane
Filtration
for
Microbial
Removal.
Report
No.
90715.
AWWARF,
Denver,
CO.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
9
Jacangelo,
J.
G,
M.
E.
Aeita,
K.
E.
Carns,
E.
W.
Cummings,
and
J.
Mallevialle.
1989a.
"
Assessing
Hollow­
Fiber
Ultrafiltration
for
Particle
Removal,"
J.
AWWA,
81:
11:
68.

Jacangelo,
J.
G.,
J.
M.
Laine,
K.
E.
Carns,
E.
W.
Cummings
and
J.
Mallevialle.
1991.
"
Low­
Pressure
Membrane
Filtration
for
Removing
Giardia
and
Microbial
Indicators,"
J.
AWWA,
83:
9:
97.

Jacangelo,
J.
G.,
J.
M.
Laine,
E.
W.
Cummings,
S.
S.
Adham.
1995.
"
UF
with
Pretreatment
for
Removing
DBP
Precursors."
J.
AWWA,
87:
3:
100.

Jacangelo,
J.
G.,
N.
L.
Patania,
K.
M.
Reagan,
E.
M.
Aieta,
S.
W.
Krasner,
and
M.
J.
McGuire.
1989b.
Ozonation:
Assessing
Its
Role
in
the
Formation
and
Control
of
Disinfection
By­
Products,"
J.
AWWA,
81:
8:
74.

Jack,
A.
M.
and
Clark,
M.
M.
1998.
"
Using
PAC­
UF
to
Treat
a
Low­
Quality
Surface
Water."
J.
AWWA,
90(
11):
83.

Jekel,
M.
R.,
and
B.
U.
Ernst.
1981.
"
Einfluss
von
huminstoffen
und
ihrer
ozonten
produkte
auf
die
electrotykoagulation
von
polystyrolatex."
Vom
Wasser,
57:
123­
126.

Jodellah,
A.
M.
and
Weber,
W.
J.
1985.
"
Controlling
Trihalomethane
Formation
Potential
by
Chemical
Treatment
and
Adsorption."
J.
AWWA,
77:
10:
95.

Johnson,
D.
E.
and
Randtke,
S.
J.
1983.
"
Removing
Non­
Volatile
Organic
Chlorine
and
Its
Precursors
by
Coagulation
and
Softenin."
J.
AWWA,
75:
5:
249.

Joret,
J.
C.,
V.
Mennecart,
C.
Robert,
B.
Campagnon
and
P.
Cervantes.
1997.
"
Inactivation
of
Indigenous
Bacteria
in
Water
by
Ozone
and
Chlorine."
Wat.
Sci.
Tech,
35:
11­
12:
81­
86.

Junli,
H.,
W.
Li,
R.
Nanqi,
M.
Fang,
and
Juli.
1997.
"
Disinfection
Effect
of
Chlorine
Dioxide
on
Bateria
in
Water."
Water
Research,
31:
3:
607­
613.

Juranek,
D.
"
Cryptosporidiosis:
Sources
of
infection
and
guidelines
for
prevention."
Clin.
Infect.
Dis.
21(
Suppl.
1)
(
1995):
S57­
S61.

Kaastrup,
E.
1985.
Activated
Carbon
Adsorption
of
Humic
Substances
and
the
Influence
of
Preozonation
on
Such.
Dissertation,
Univ.
Trondheim,
Norwegian
Inst.
Technol.,
Trondheim,
Norway.

Karimi,
A.,
Vickers,
J.,
Harasick,
R.
1999.
"
Microfiltration
goes
Hollywood:
the
Los
Angeles
Experience."
J.
AWWA,
91:
6:
90­
103.

Kashinkunti,
R.,
K.
G.
Linden,
G.
Shin,
D.
H.
Metz,
M.
D.
Sobsey,
M.
Moran,
and
A.
Samuelson.
2003.
Achieving
multi­
barrier
inactivation
in
Cincinnati:
UV,
byproducts,
and
biostability.
J.
AWWA.
Submitted
January
9,
2003.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
10
Katzenelson,
E.,
Kletter,
E.,
Schechter,
H.,
and
Shuval,
H.
1974.
"
Inactivation
of
Viruses
and
Bacteria
by
Ozone."
J.
AWWA,
66:
725­
729.

Kavanaugh,
M.
C.
1978.
"
Modified
Coagulation
for
Improved
Removal
of
Trihalomethane
Precursors."
J.
AWWA,
70:
11:
613.

Kawamura,
S.
2000.
Integrated
Design
and
Operation
of
Water
Treatment
Facilities.
2nd
Edition,
John
Wiley
&
Sons,
New
York,
NY.

Keller,
J.
W.,
Morin,
R.
A.,
and
Scaffernoth,
T.
J.
1974.
"
Ozone
Disinfection
Pilot
Plant
Studies
at
Laconia,
NH."
J.
AWWA,
66:
7:
30.

Kinman,
R.
N.
(
1975).
"
Water
and
Wastewater
Disinfection
With
Ozone,"
Crit.
Rev.
Environ.
Control,"
5:
1:
141­
152.

Kirmeyer,
G.
J.,
G.
W.
Foust,
G.
L.
Pierson,
J.
J.
Simmler,
M.
W.
LeChevallier.
1993.
Optimizing
Chloramine
Treatment,
Report
No.
90620.
AWWARF,
Denver,
CO.
Kirmeyer,
G.
J.,
L.
H.
Odell,
J.
G.
Jacangelo,
A.
Wilczak,
and
R.
Wolfe.
1995.
Nitrification
Occurrence
and
Control
in
Chloraminated
Water
Systems.
Report
No.
90669.
AWWARF,
Denver,
CO.

Kittridge,
D.,
Beaurivage,
R.
and
Paris,
D.
1983.
Granular
Activated
Carbon
Adsorption
and
Fluid­
Bed
Reactivation
at
Manchester,
New
Hampshire.
USEPA
Rpt.
No.
EPA/
600/
2­
83/
104.
Cincinnati,
OH.

Knocke,
W.
R.
West,
S.
and
Hoehn,
R.
C.
1986.
"
Effects
of
Low
Temperature
on
the
Removal
of
Trihalomethane
Precursors
by
Coagulation."
J.
AWWA,
78:
4:
189.

Knudson,
G.
B.
1985.
Photoreactivation
of
UV­
irradiated
Legionella
Pneumoplila
and
other
Legionella
species.
Applied
and
Environmental
Microbiology
49,
No.
4:
975­
980.

Koffskey,
W.
E.
1987.
Alternative
Disinfectants
and
Granular
Activated
Carbon
Effects
on
Trace
Organic
Contaminants.
USEPA
Rpt.
No.
EPA/
600/
2­
87/
006,
Cincinnati,
OH.

Korich,
D.
G.,
J.
R.
Mead,
M.
S.
Madore,
N.
A.
Sinclair,
and
C.
R.
Sterling.
1990.
"
Effects
of
Ozone,
Chlorine
Dioxide,
Chlorine,
and
Monochloramine
on
Cryptosporidium
parvum
Oocyst
Viability."
Applied
Engineering
and
Microbiology.
56:
5:
1423­
1428.

Kornegay,
B.
H.
1979.
"
Control
of
Synthetic
Organic
Chemicals
of
Activated
Carbon
 
Theory,
Application
and
Regeneration
Alternatives."
Presented
at
the
Seminar
on
Control
of
Organic
Chemicals
in
Drinking
Water,
sponsored
by
USEPA.

Krasner,
S.
et
al.
1996.
Issue
paper
prepared
during
USEPA
Technologies
Working
Group
Meetings.

Krasner,
S.
W.,
et
al.
1989.
"
The
Occurrence
of
Disinfection
By­
Products
in
U.
S.
Drinking
Water,
"
J.
AWWA,
81:
8:
41.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
11
Krasner,
S.
W.,
W.
H.
Glaze,
H.
S.
Weinberg,
P.
A.
Daniel,
and
I.
N.
Najm.
1993.
"
Formation
and
Control
of
Bromate
During
Ozonation
of
Waters
Containing
Bromide,"
J.
AWWA,
85:
1:
73.

Kruithof,
J.
C.
P.
Hiemstra,
P.
Kamp,
J.
van
der
Hoek,
and
J.
C.
Schippers.
1997.
"
Integrated
Multi­
Objective
Membrane
Systems
for
Control
of
Microbials
and
DBP­
Precursors,"
AWWA
Membrane
Technology
Conference
Proceedings,
February
23­
26,
1997,
New
Orleans,
LA.

Laine,
J.
M.,
Clark,
M.
M.
and
Mallevialle,
J.
1990.
"
Ultrafiltration
of
Lake
Water:
Effect
of
Pretreatment
On
The
Partitioning
Of
Organics,
THMFP
Flox."
J.
AWWA,
82:
12:
82.

Langlais,
B.
et
al.
1990.
"
New
Developments:
Ozone
in
Water
and
Wastewater
Treatment.
The
CT
Value
Concept
for
Evaluation
of
Disinfection
Process
Efficiency;
Particular
Case
of
Ozonation
for
Inactivation
of
Some
Protozoa,
Free­
Living
Amoeba
and
Cryptosporidium."
IOA
Pan­
American
Conference,
Shreveport,
LA.

Langlais,
B.;
Reckhow,
D.
A.;
Brink,
D.
R.
(
Editors).
1991.
Ozone
in
Drinking
Water
Treatment:
Application
and
Engineering.
AWWARF,
Compagnie
Generale
Des
Eaux,
Lewis
Publishers,
Chelsea,
MI.

Laurent,
P.,
Servais,
P.,
Gatel,
D.,
Randon,
G.,
Bonne,
P.,
Cavard,
J.
1999.
"
Microbiological
Quality
Before
and
After
Nanofiltration."
J.
AWWA,
91:
10:
62.

Lebeau,
T.,
Lelievre,
C.,
Buisson,
H.,
Cleret,
D.,
Van
de
Venter,
L.,
Cote,
P.
1998.
"
Immersed
Membrane
Filtration
for
the
Production
of
Drinking
Water:
Combination
with
PAC
for
NOM
and
SOCs
Removal."
Desalination,
117:
219­
231.

LeChevallier,
M.
W.
1998.
"
Benefits
of
Employing
a
Disinfectant
Residual
in
Distribution
Systems,"
Water
Supply,
16:
3­
4:
61­
73.

LeChevallier,
M.
W.,
W.
D.
Norton,
and
R.
G.
Lee.
1991.
"
Evaluation
of
a
Method
to
Detect
Giardia
and
Cryptosporidium
in
Water."
From
Monitoring
Water
in
the
1990'
s:
Meeting
New
Challenges.
ASTM
STP
1102
J.
R.
Hall
and
G.
D.
Glysson,
eds.
American
Society
for
Testing
and
Materials,
Philadelphia.

Lee,
M.
C.,
Crittenden,
J.
C.,
Snoeyink,
V.
L.
and
Ari,
M.
1983.
"
Design
of
Carbon
Beds
to
Remove
Humic
Substances."
J.
Env.
Eng.,
109:
3:
631.

Lee,
M.
C.,
Snoeyink,
V.
L.
and
Crittenden,
J.
C.
1981.
"
Activated
Carbon
Adsorption
of
Humic
Substances."
J.
AWWA,
73:
8:
440.

Lee,
Y.
and
Hunter,
J.
V.
1985.
"
Effect
of
Ozonation
and
Chlorination
on
Environmental
Protection
Agency
Priority
Pollutants."
Water
Chlorination:
Chemistry,
Environmental
Impact
and
Health
Effects.
Vol.
5.
R.
L.
Jolley,
R.
J.
Bull,
W.
P.
Davis,
S.
Katz,
M.
H.
Roberts
and
V.
A.
Jacobs(
eds).
Lewis
Publishers,
p.
1515.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
12
Legube,
B.,
Agbekodo,
K.,
Cote,
P.,
Bourbigot,
M.
1995.
"
Removal
of
Organohalide
Precursors
by
Nanofiltration."
Water
Supply,
13:
2:
171­
181.

Leinhard,
H.
and
Sontheimer,
H.
1979.
"
Influence
of
Process
Conditions
on
the
Effect
of
Ozone
Treatment
of
Organic
Substances
in
Water."
Ozone
Sci.
Eng.,
1:
1:
61.

Li,
H.,
G.
R.
Finch,
N.
Neumann,
and
M.
Belosevic.
1998.
"
Inactivation
of
Cryptosporidium
by
Chlorine
Dioxide
at
1oC."
Water
Quality
Technology
Conference
Proceedings,
AWWA,
San
Diego,
CA.

Li,
S.
Y.,
J.
A.
Goodrich,
J.
H.
Owens,
G.
E.
Willeke,
F.
W.
Schaefer
and
R.
M.
Clark.
1997.
"
Reliability
of
Surrogates
for
Determining
Cryptosporidium
Removal,"
J.
AWWA,
89:
5:
90­
99.

Liao,
M.
Y.
and
Randtke,
S.
J.
1985.
"
Removing
Fulvic
Acid
by
Lime
Softening."
J.
AWWA,
77:
8:
78.

Linden,
K.
G.
2002.
Personal
email
communication
by
Laurel
Passantino.
April
24­
May
6.

Linden,
K.
G.,
L.
Batch,
and
C.
Schulz.
2002b.
UV
Disinfection
of
filtered
water
supplies:
water
quality
impacts
on
MS2
dose­
response
curves.
Proceedings
of
the
AWWA
Annual
Conference,
June
16­
20,
New
Orleans,
LA.

Linden,
K.
G.,
G.
A.
Shin,
G.
Faubert,
W.
Cairns,
and
M.
D.
Sobsey.
2002a.
UV
disinfection
of
Giardia
lamblia
cysts
in
water.
Environmental
Science
and
Technology
36,
No.
11:
2519­
2522.
Linden,
K.
G.,
G.
S.
Soriano,
and
J.
L.
Darby.
1998.
"
Investigation
of
Disinfection
Byproduct
Formation.
Following
Low
and
Medium
Pressure
UV
Irradiation
of
Wastewater."
WEF
Disinfection
Conference
Proceedings.

Lindenauer
K.
and
J.
Darby.
1994.
"
Ultraviolet
disinfection
of
wastewater:
Effect
of
Dose
on
Subsequent
Photoreactivation."
Water
Research,
28:
4:
805­
817.

Liyanage,
L.
R.
J.,
G.
R.
Finch,
and
M.
Belosevic.
1997a.
"
Synergistic
Effects
of
Sequential
Exposure
of
Cryptosporidium
Oocysts
to
Chemical
Disinfectants,"
1997
International
Symposium
on
Waterborne
Cryptosporidium
Proceedings,
March
2­
5,
1997,
Newport
Beach,
CA,
AWWA,
Denver,
CO.

Liyanage,
L.
R.
J.,
G.
R.
Finch,
and
M.
Belosevic.
1997b.
"
Sequential
Disinfection
of
Cryptosporidium
parvum
by
Ozone
and
Chlorine
Dioxide,"
Ozone
Sci.
Eng.,
19:
409­
423.

Long,
W.
R.
1983.
"
Evaluation
of
Cartridge
Filters
for
the
Removal
of
Giardia
lamblia
Cyst
Models
from
Drinking
Water
Systems."
J.
Env.
Health,
45:
5:
220­
225.

Lozier,
J.
1998.
"
Implementation
of
Integrated
Membrane
Treatment:
Lessons
Learned
from
Three
years
of
Operation
in
Barrow,
Alaska."
Microfiltration
II
Conference
of
the
National
Water
Research
Institute
Proceedings,
San
Diego,
CA.

Lozier,
J.,
Jones,
G.,
Bellamy,
W.
1997.
"
Integrated
Membrane
Treatment
in
Alaska."
J.
AWWA,
89:
10:
50.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
13
Luitweiler,
J.
P.,
T.
L.
Yohe,
E.
Crist,
and
X.
Sun.
1991.
"
Performance
Testing
of
Hollow­
Fiber
Membranes
on
a
Groundwater,"
AWWA
Membrane
Technology
Conference,
Proceedings,
Orlando,
FL.

Lykins,
B.
W.
and
Griese,
M.
H.
1986.
"
Using
Chlorine
Dioxide
for
Trihalomethane
Control."
J
AWWA,
78:
6:
88.

Mackey,
E.
D.;
Cushing,
R.
S.;
&
G.
F.
Crozes.
2000.
UV
Disinfection
Systems
for
the
Inactivation
of
Cryptosporidium:
Evaluating
Practical
Implementation
Issues.
Proceedings,
2000
Annual
AWWA
Conference,
Denver,
CO.

Malcolm
Pirnie,
Inc.
1988.
Unpublished
data.

Malcolm
Pirnie,
Inc.
1989.
Water
Quality
Master
Plan.
Prepared
for
City
of
Phoenix,
AZ.

Malcolm
Pirnie,
Inc.
1990.
City
of
San
Diego
Water
Quality
Report,
August
1990.

Malcolm
Pirnie,
Inc.
1993.
Very
Small
Systems
Best
Available
Technology
Cost
Document.
Prepared
for
USEPA
Office
of
Ground
Water
and
Drinking
Water.

Mallevialle,
J.,
P.
E.
Odendaal,
and
M.
R.
Weisner,
ED.
1996.
Water
Treatment
Membrane
Processes.
AWWARF.
Lyonnaise
des
Eaux,
Water
Research
Commission
of
South
Africa.
McGraw
Hill.

Malley,
J.
P.,
J.
P.
Show,
and
J.
R.
Ropp.
1996.
Evaluation
of
Byproducts
Produced
by
Treatment
of
Groundwaters
with
Ultraviolet
Irradiation.
Report
No.
90685.
AWWARF
&
AWWA,
Denver,
CO.

Malley,
J.
P,
J.
P.
Shaw
and
J.
R.
Ropp.
1995.
Evaluation
of
by­
products
produced
by
treatment
of
groundwaters
with
ultraviolet
irradiation.
Denver,
CO.:
AWWA
Research
Foundation.

Malley,
J.
R.
1999.
"
UV
Disinfection's
Emerging
Role
in
Drinking
Water
Treatment
 
Theories
and
Practical
Questions."
USEPA
Workshop
on
UV
Disinfection
of
Drinking
Water,
April
28­
29,
1999,
Arlington,
VA.

Malley,
J.
R.
1998.
Control
of
Microbes
in
Drinking
Water,
Chapter
13:
Ultraviolet
Disinfection.
Draft
Chapter
from
ASCE
Manual.

Maloney,
S.
W.,
Suffet,
I.
H.,
Bancroft,
K.
and
Neukrug,
H.
M.
1985.
"
Ozone­
GAC
Following
Conventional
US
Drinking
Water
Treatment."
J.
AWWA,
77:
8:
66.

Marinas,
J.
B.,
Rennecker,
L.
J.,
Teefy,
S.,
and
Rice
W.
E.
1999.
"
Assessing
Ozone
Disinfection."
J.
AWWA,
91:
10:
79.

Marriott,
W.
D.,
M.
M.
Clark,
J.
M.
Laine.
1997.
"
Piloting
for
Optimal
Operation
of
Ultrafiltration."
Annual
AWWA
Membrane
Conference
Proceedings,
New
Orleans,
LA.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
14
McCreary,
J.
J.
and
Snoeyink,
V.
L.
1980.
"
Characterization
and
Activated
Carbon
Adsorption
of
Several
Humic
Substances."
Water
Research,
14:
1:
151.

McGuire,
M.
J.,
Davis,
M.
K.,
Liang,
S.,
Tate,
C.
H.,
Aieta,
E.
M.,
Wallace,
I.
E.,
Wilkes,
D.
R.,
Crittenden,
J.
C.
and
Vaith,
K.
1989.
Optimization
and
Economic
Evaluation
of
Granular
Activated
Carbon
for
Organic
Removal,
AWWA
Research
Foundation,
Denver,
CO.

McGuire,
M.
J.;
Krasner,
S.
W.;
Gramith,
J.
T.
1990.
Comments
on
Bromide
Levels
in
State
Project
Water
and
Impacts
on
Control
of
Disinfection
Byproducts.

McGuire,
M.
J.,
Krasner,
S.
W.,
Reagan,
K.
M.,
Aieta,
E.
M.,
Jacangelo,
J.
G.,
Patania,
N.
L.
and
Gramith,
K.
M.
1989.
Disinfection
By­
Products
in
United
States
Drinking
Waters.
Final
Report
for
the
USEPA
and
AMWA.

McTigue,
N.
E.,
M.
LeChevallier,
H.
Arora,
J.
Clancy.
1998.
National
Assessment
of
Particle
Removal
by
Filtration.
Denver:
American
Water
Works
Association
Research
Foundation
and
AWWA.
p.
266
Meals,
D.
W.
2001.
"
Water
quality
response
to
riparian
restoration
in
an
agricultural
watershed
in
Vermont,
USA."
Water
Sci.
Technology,
43(
5):
175­
82.

Medema,
G.
J.,
M.
H.
A.
Juhasz­
Hoterman,
and
J.
A.
Luitjen.
2000.
"
Removal
of
microorganisms
by
bank
filtration
in
a
gravel­
sand
soil."
Proceedings,
International
Riverbank
Filtration
Conference,
November
2­
4,
Düsseldorf.
W.
Julich
and
J.
Schubert,
eds.
Internationale
Arbeitgemeinschaft
der
Wasserwerke
im
Rheineinzugsgebiet,
Amsterdam,
pp.
161­
168.
Meng,
Q
and
C.
Gerba.
1996.
"
Comparative
Inactivation
of
Enteric
Adenoviruses,
Poliovirus
and
Coliphages
by
Ultraviolet
Irradiation."
Water
Research,
30:
11:
2665­
2668.

Miller,
R.
and
Hartman,
D.
J.
1982.
Feasibility
of
Granular
Activated
Carbon
and
On­
Site
Reactivation.
USEPA
Rpt.
No.
EPA/
600/
2­
82/
087,
Cincinnati,
OH.

Miltner,
R.,
Rice
E.
W.
and
Stevens,
A.
A.
1990.
"
A
Study
of
Ozone's
Role
in
Disinfection
By­
Product
Control."
Presented
at
the
1990
Spring
Conference
of
the
International
Ozone
Association,
Shreveport,
LA.

Mofidi,
A.
1999.
"
Inactivation
of
Cryptosporidium
parvum
with
Polychromatic
UV
Systems
 
Water
Quality
Monitoring."
USEPA
Workshop
on
UV
Disinfection
of
Drinking
Water,
April
28­
29,
1999,
Arlington,
VA.

Montgomery,
James
M.,
Consulting
Engineers,
Inc.
1992.
Effect
of
Coagulation
and
Ozonation
on
the
Formation
of
Disinfection
Byproducts.
Prepared
for
the
AWWA.

Mulford,
L.,
Taylor,
J.,
Nickerson,
D.,
Chen,
S­
S.
1999.
"
NF
Performance
at
Full
and
Pilot
Scale."
J.
AWWA,
91:
6:
64.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
15
Najm,
I.
N
and
S.
W.
Krasner.
1995.
"
Effects
of
Bromide
and
Natural
Organic
Matter
on
the
Formation
of
Ozonation
By­
Products,"
J.
AWWA,
87:
1.

Nakatsuka,
S.,
Nakate,
I.,
Miyano,
T.
1996.
"
Drinking
Water
Treatment
by
Using
Ultrafiltration
Hollow
Fiber
Membranes."
Desalination,
106:
55­
61.

Neukrug,
H.
M.,
et
al.
1983.
Removing
Organics
From
Philadelphia
Drinking
Water
by
Combined
Ozonation
and
Adsorption.
USEPA
Municipal
Environmental
Research
Laboratory,
Cincinnati,
OH.
Rpt.
No.
EPA/
600/
S2­
83/
048,
NTIS
Publ.
No.
PB83­
223370.

Neukrug,
H.
M.,
Smith,
M.
G.,
Maloney,
S.
W.
and
Suffet,
I.
H.
1984.
"
Biological
Activated
Carbon
­
At
What
Cost?"
J.
AWWA,
76:
4:
158.

Nowack,
K.
O.,
F.
S.
Cannon,
and
H.
Arora.
1999.
"
Ferric
Chloride
plus
GAC
for
Removing
TOC."
J.
AWWA,
91:
2:
65­
78.

Oguma
K.,
H.
Katayama,
H.
Mitani,
S.
Morita,
T.
Hirata,
and
S.
Ohgaki.
2001.
Determination
of
pyrimidine
dimers
in
Escherichia
coli
and
Cryptosporidium
parvum
during
UV
light
inactivation,
photoreactivation
and
dark
repair.
Applied
and
Environmental
Microbiology
67,
No.
10:
4630­
4637.

Olivieri,
V.,
Parker
Jr.,
D.,
Willinghan,
G.,
Vickers,
J.
1991.
"
Continuous
Microfiltration
of
Surface
Water."
AWWA
Membrane
Technology
Conference
Proceedings,
Orlando,
FL.

Owens,
J.
H.
et.
al.
1994.
"
Pilot­
Scale
Ozone
Inactivation
of
Cryptosporidium
and
Giardia."
WQTC,
San
Francisco,
CA.

Parrotta,
M.
J.
and
F.
Bekdash.
1998.
"
UV
Disinfection
for
Small
Groundwater
Supplies."
J.
AWWA,
90:
2:
71­
81.

Passantino,
L.
B.
and
J.
P.
Malley.
2001.
Impacts
of
turbidity
and
algal
content
of
unfiltered
drinking
water
supplies
on
the
ultraviolet
disinfection
process.
Proceedings
of
the
2001
AWWA
Annual
Conference,
Washington,
DC.

Patania,
N.
L.,
J.
G.
Jacangelo,
L.
Cummings,
A.
Wilczak,
K.
Riley,
and
J.
Oppenheimer.
1995.
"
Optimization
of
Filtration
for
Cyst
Removal."
Denver:
AWWA
Research
Foundation
and
AWWA.

Payment,
Pierre,
and
E.
Franco.
1993.
"
Clostridium
perfringens
and
somatic
coliphages
as
indicators
of
the
efficiency
of
drinking
water
treatment
for
viruses
and
protozoan
cysts."
Applied
and
Environmental
Microbiology.
59
(
8):
2418­
2424.

Peeters,
J.
E.
et
al.
1989.
"
Effect
of
Disinfection
of
Drinking
Water
with
Ozone
or
Chlorine
Dioxide
on
Survival
of
Cryptosporidium
Parvum
Oocysts."
Applied
and
Environmental
Microbiology,
55:
6:
1519­
1522.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
16
Pontius,
F.
W.
and
W.
R.
Diamond.
1999.
"
Complying
with
the
Stage
1
D/
DBP
Rule."
J.
AWWA,
91:
3:
16­
32.

Prados­
Ramirez,
M.,
Ciba,
N.,
Bourbigot,
M.
1993.
"
Available
Techniques
for
Reducing
Bromate
in
Drinking
Water."
International
Water
Supply
Association
International
Conference
Proceedings:
Bromate
and
Water
Treatment,
Paris,
France.

Prengle,
H.
W.,
Mauk,
C.
E.
and
Payne,
J.
E.
1976.
"
Ozone/
UV
Oxidation
of
Chlorinated
Compounds
in
Water."
Presented
at
the
International
Ozone
Institute
Forum
on
Ozone
Disinfection.
Chicago,
IL.

Quinonez­
Diaz,
M.
J.,
M.
M.
Karpiscak,
E.
D.
Ellman,
and
C.
P.
Gerba.
2001.
"
Removal
of
pathogenic
and
indicator
moicroorganisms
by
a
constructed
wetland
receiving
untreated
domestic
wastewater."
Journal
of
Environmental
Science
and
Health,
Part
A,
Toxic/
Hazardous
Substances
and
Environmental
Engineering,
36(
7):
1311­
20.

Randtke,
S.
J.
1988.
"
Organic
Contaminant
Removal
by
Coagulation
and
Related
Process
Combinations."
J.
AWWA,
80:
5:
40.

Randtke,
S.
J.,
Thiel,
C.
E.,
Liao,
M.
Y.
and
Yamaya,
C.
N.
1982.
"
Removing
Soluble
Organic
Contaminants
by
Lime­
Softening."
J.
AWWA,
74:
4:
192.

Randtke,
S.
J.
and
Jepsen,
C.
P.
1981.
"
Chemical
Pretreatment
for
Activated
Carbon
Absorption."
J.
AWWA,
73:
8:
411.

Randtke,
S.
J.
and
Jepsen,
C.
P.
1982.
"
Effects
of
Salts
on
Activated
Carbon
Adsorption
of
Fulvic
Acids."
J.
AWWA,
74:
2:
84.

Rauth,
A.
M.
1965.
The
physical
state
of
viral
nucleic
acid
and
the
sensitivity
of
viruses
to
ultraviolet
light.
Biophysical
Journal
5:
257­
273.

Reckhow,
D.
A.
and
Singer,
P.
C.
1984.
"
The
Removal
of
Organic
Halide
Precursors
by
Preozonation
and
Alum
Coagulation."
J.
AWWA,
76:
4:
151.

Reckhow,
D.
A.
and
Singer,
P.
C.
1990.
"
Chlorination
By­
Products
in
Drinking
Waters:
From
Formation
Potentials
to
Concentrations
in
the
Finished
Water."
J.
AWWA,
82:
4.

Reed,
G.
D.
1983.
"
Effects
of
Prechlorination
on
THM
Formation
and
Microbial
Growth
in
Pilot­
Plant
Units."
J.
AWWA,
82:
4:
426.

Rennecker,
J.
L.,
B.
Corona­
Vasquez,
A.
M.
Driedger
and
B.
J.
Marinas.
2000.
"
Synergism
in
Sequential
Disinfection
of
Cryptosporidium
parvum."
Wat.
Sci.
Tech.,
41:
7:
47­
52.

Rennecker,
J.
L.,
Marinas,
J.
B.,
Owens,
H.
J.,
and
Rice,
W.
E.
1999.
"
Inactivation
of
Cryptosporidium
Parvum
Oocysts
With
Ozone."
Water
Resources,
33:
11:
2481­
2488.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
17
Rice,
E.
W.
and
J.
C.
Hoff.
1981.
"
Inactivation
of
Giardia
lamblia
Cysts
by
Ultraviolet
Irradiation."
Appl.
and
Environ.
Microbiol.
42:
3:
546­
547.

Rice,
R.
G.,
P.
K.
Overbeck
and
K.
O.
Larson.
1999.
"
Ozone,
an
Effective
and
Affordable
Choice
for
Small
Water
Systems."
1999
AWWA
Annual
Conference
Proceedings,
Chicago,
IL.

Robeck,
G.
G.,
K.
A.
Dostal
and
R.
L.
Woodward.
1964.
"
Studies
of
Modifications
in
Water
Filtration."
J.
AWWA,
56:
2:
198­
213.

R.
S.
Means
Company
Inc.
1999.
RSMeans
Facilities
Construction
Cost
Data,
14th
annual
ed.
Kingston,
MA.

SAB
and
USEPA.
1990.
Reducing
risk:
setting
priorities
and
strategies
for
environmental
protection.
Washington,
DC.:
U.
S.
EPA
Science
Advisory
Board.
SAB­
EC­
90­
021.

Scanlan,
P.,
Pohlman,
B.,
Freeman,
S.,
Spillman,
B.,
Mark,
J.
1997.
"
Membrane
Filtration
for
the
Removal
of
Color
and
TOC
from
Surface
Water."
AWWA
Membrane
Technology
Conference
Proceedings,
New
Orleans,
LA.

Schneider,
O.
D.,
E.
Acs,
Leggerio,
and
S.
Nickols
(
1999).
"
The
Use
of
Microfiltration
for
Backwash
Water
Treatment,"
AWWA
Annual
Conference
Proceedings,
June
20
­
24,
1999,
Chicago,
IL.

Semmens,
M.
J.
and
Ayers,
K.
1985.
"
Removal
by
Coagulation
of
Trace
Organics
from
Mississippi
River
Water."
J.
AWWA,
77:
5:
79.

Semmens,
M.
J.,
Norgaard,
G.
E.,
Hohenstein,
G.
and
Staples,
A.
B.
1986.
"
Influence
of
pH
on
the
Removal
of
Organics
by
Granular
Activated
Carbon."
J.
AWWA,
78:
5:
89.

Semmens,
M.
J.
and
Staples,
A.
B.
1986.
"
The
Nature
of
Organics
Removed
During
Treatment
of
Mississippi
River
Water."
J.
AWWA,
78:
2:
76.

Semmens,
M.
J.
and
T.
K.
Field.
1980.
"
Coagulation:
Experiences
in
Organics
Removal."
J.
AWWA,
72:
8:
476.

Seyde,
V.,
D.
Clark,
E.
Akiyoshi,
A.
Kalinsky,
and
C.
Spangenberg.
1999.
"
Nanofiltration
Process
Microbial
Challenge
Studies,"
AWWA
Membrane
Technology
Conference
Proceedings,
February
28
­
March
3,
1999,
Long
Beach,
CA.

Shaban,
A.
M.,
G.
E.
El­
Taweel,
and
G.
H.
Ali.
1997.
UV
Ability
to
Inactivate
Microorganisms
Combined
with
Factors
Affecting
Radiation.
Wat.
Sci.
Tech.,
35:
11­
12:
107­
112.

Shin
G.
A.,
K.
G.
Linden,
M.
J.
Arrowood,
G.
Faubert,
and
M.
D.
Sobsey.
2001.
DNA
repair
of
UVirradiated
Cryptosporidium
parvum
oocysts
and
Giardia
lamblia
cysts.
Proceedings
of
the
First
International
Ultraviolet
Association
Congress,
June
14­
16,
Washington,
D.
C.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
18
Shin,
G.,
K.
G.
Linden,
G.
Faubert,
M.
Arrowood,
and
M.
D.
Sobsey.
2000a.
"
Inactivation
of
Cryptosporidium
parvum
Oocysts
and
Giardia
lamblia
Cysts
by
Monochromatic
UV
Radiation."
Proceedings
of
the
IWA
First
International
Congress,
Health
Related
Microbiology,
Paris,
July
1­
4,
2000.

Shin,
G.
A.,
Linden,
K.
G.,
and
Sobsey,
M.
D.
2000b.
Comparative
Inactivation
of
Cryptosporidium
Parvum
Oocysts
and
Coliphage
MS­
2
by
Monochromatic
UV
Radiation.
Proc.,
Disinfection
2000,
WEF
Specialty
Conference,
New
Orleans,
LA.
March
15­
17,
2000.

Shukairy,
H.
M.
and
Summers,
R.
S.
1990.
"
The
Impact
of
Preozonation
and
Biodegradation
on
the
Formation
of
Halogenated
Organic
Compounds
After
Chlorination
And
Chloramination."
AWWA
Annual
Conference,
Cincinnati,
OH.

Siddiqui,
M.
S.,
G.
L.,
Amy,
and
McCollum,
L.
J.
1996.
"
Bromate
Destruction
by
UV
Irradiation
and
Electric
Arc
Discharge."
J.
Ozone
S&
E,
18:
271­
290.

Siddiqui,
M.
S.,
G.
L.
Amy
and
R.
Rice.
1995.
"
Bromate
Ion
Formation
in
Drinking
Water:
A
Critical
Review."
J.
AWWA,
87:
10:
58.

Siddiqui,
M.
S.
and
G.
L.
Amy.
1993.
"
Factors
Affecting
DBP
Formation
During
Ozone­
Bromide
Reactions."
J.
AWWA,
85:
1:
63­
72.

Singer,
P.
C.
1988.
Alternative
Oxidant
and
Disinfectant
Treatment
Strategies
for
Controlling
Trihalomethane
Formation.
USEPA
Risk
Reduction
Engineering
Laboratory,
Cincinnati,
OH.
Rpt.
No.
EPA/
600/
2­
88/
044,
NTIS
Publ.
No.
PB88­
238928.

Singer,
P.
C.
and
Chang,
S.
D.
1988.
"
Characterization
of
the
Impact
of
Pre­
Ozonation
of
Raw
Drinking
Water."
Presented
at
the
1988
Spring
Technical
Conference
of
the
International
Ozone
Assoc.,
Monroe,
MI.

Sinsabaugh,
R.
L.,
Hoehn,
R.
C.,
Knocke,
W
R.
and
Linkins,
A.
E.
1986a.
"
Removal
of
Dissolved
Organic
Carbon
by
Coagulation
with
Iron
Sulfate."
J.
AWWA,
78:
5:
74.

Sinsabaugh,
R.
L.,
Hoehn,
R.
C.,
Knocke,
W.
R.
and
Linkins,
A.
E.
1986b.
"
Precursor
Size
and
Organic
Halide
Formation
Rates
in
Raw
and
Coagulated
Surface
Waters."
J.
Env.
Eng.,
111:
6:
850.

Solarik
G.,
Hooper
S.
M.,
Summers
R.
S.,
Owen
D.
M.
1996.
"
The
Impact
of
Ozonation
and
Biotreatment
on
GAC
Performance
for
NOM
Removal
and
DBP
Control."
American
Water
Works
Association
Conference
Proceedings,
Toronto,
Ontario,
Canada.

Solo­
Gabriele,
H.,
and
S.
Neumeister.
1996.
"
U.
S.
Outbreaks
of
Cryptosporidiosis."
J.
AWWA
88:
76­
86.

Somiya,
I.,
Yamada,
H.,
Nozawa,
E.
and
Mohri,
M.
1986.
"
Biodegradability
and
GAC
Adsorbability
of
Micropollutants
by
Preozonation."
Ozone
Sci.
Eng,
8:
1:
11.

Song,
R.,
R.
Minear,
P.
Westerhoff,
and
G.
Amy
(
1995).
"
Bromate
Formation
and
Minimization
in
Water
Treatment,"
AWWA
Water
Quality
Technology
Conference
Proceedings,
New
Orleans,
LA.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
19
Soroushian,
F.
and
W.
D.
Bellamy.
2000.
"
Assessment
of
Ultraviolet
Technology
for
Drinking
Water
Disinfection:
Facts
of
Light."
Proceedings
of
the
2000
AWWA
Annual
Conference,
Denver,
CO.

Spangenberg,
C.,
E.
Akiyoshi,
A.
Kalinsky,
V.
Seyde,
D.
Clark
and
J.
Taylor.
1999.
"
Insights
on
Recent
Membrane
Integrity
Testing
of
an
Organic
Selective
Nanofiltration
and
Hybrid
Membrane
Arrangement,"
AWWA
Membrane
Technology
Conference
Proceedings,
February
28
­
March
3,
1999,
Long
Beach,
CA.

Speitel,
G.
E.,
Turakhia,
M.
H.
and
Lu,
C.
J.
1989.
"
Initiation
of
Micropollutant
Biodegradation
in
Virgin
GAC
Columns."
J.
AWWA,
81:
4:
168.

Speitel,
G.
E.,
Patterson,
A.
M.,
Lu,
C.
J.
and
Thompson,
R.
C.
1989.
"
Aerobic
Biodegradation
of
Chloroform
and
Trichloroethylene
in
Drinking
Water
Treatment."
AWWA
Annual
Conference
Proceedings,
Los
Angeles,
CA.

Spencur,
C.
M.
and
Collins,
M.
R.
1990.
"
Modifications
of
Precoat
Filter
with
Crushed
Granular
Activated
Carbon
and
Amiona
Resin
Improves
Organic
Precursor
Removal."
1990
AWWA
Annual
Conference
Proceedings,
p.
509.

Staehlin,
J.
and
Hoigne,
J.
1983.
Vom
Wasser.
61:
337.

Staehlin,
J.
and
Hoigne,
J.
1985.
"
Decomposition
of
Ozone
in
the
Presence
of
Organic
Solutes
Acting
as
Promoters
and
Inhibitors
of
Radical
Chain
Reactions."
Environ.
Sci.
Tech.,
19:
1206.

Stevens,
A.
A.,
Moorek,
L.
A.
and
Miltner,
R
J.
1989.
"
Formation
and
Control
of
Non­
Trihalomethane
By­
Products."
J.
AWWA,
81:
8:
54.

Summers,
R.
S.
1986.
Activated
Carbon
Adsorption
of
Humic
Substances:
Effect
of
Molecular
Size
and
Heterodispersity.
Ph.
D.
Dissertation,
Stanford
Univ.,
Stanford,
CA.

Summers,
R.
S.
et
al.
1997.
"
Removal
of
DBP
Precursors
by
Granular
Activated
Carbon
Adsorption."
AWWA
Research
Foundation,
Denver,
CO.

Summers,
R.
S.,
Hong,
S.,
Hooper,
S.,
Solarik
,
G.
1994.
"
Adsorption
of
Natural
Organic
Matter
and
Disinfection
By­
Product
Precursors."
American
Water
Works
Association
Annual
Conference
Proceedings,
New
York,
NY.

Summers,
R.
S.
and
Roberts,
P.
V.
1988.
"
Activated
Carbon
Adsorption
of
Humic
Substances.
II.
Size
Exclusion
and
Electrostatic
Interactions."
J.
Colloid
Interface
Sci.,
122:
2:
382.

Summers,
R.
S.
and
Roberts,
P.
V.
1982.
"
Performance
of
Granular
Activated
Carbon
for
Total
Organic
Carbon
Removal."
J.
AWWA.,
74:
2:
113­
118.

Symons,
J.
M.,
G.
E.
Speitel,
C.
Hwang,
S.
W.
Krasner,
and
S.
E.
Barrett.
1998.
Factors
Affecting
Disinfection
Byproduct
Formation
During
Chloramination.
AWWARF,
Denver,
CO.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
20
Symons,
J.
M,
G.
E.
Speitel,
C.
J.
Hwang,
S.
W.
Krasner,
S.
E.
Barrett,
A.
C.
Diehl,
and
R.
Xia.
1996.
"
Factors
Affecting
Disinfection
By­
Product
Formation
During
Chloramination,"
AWWA
Water
Quality
Technology
Conference
Proceedings,
Boston,
MA.

Taylor,
J.
S.,
L.
A.
Mulford,
S.
J.
Duranceau
and
W.
M.
Barret.
1989.
"
Cost
and
Performance
of
a
Membrane
Pilot
Plant."
J.
AWWA,
81:
11:
52.

Taylor,
J.
S.
D.
M.
Thompson
and
J.
K
Carswell.
1987.
"
Applying
Membrane
Processes
to
Groundwater
Sources
for
Trihalomethane
Precursor
Control."
J.
AWWA,
79:
8:
72
Thurston,
J.
A.,
C.
P.
Gerba,
K.
E.
Foster,
M.
M.
Karpiscak.
2001.
"
Fate
of
indicator
microorganisms,
Giardia,
and
Cryptosporidium
in
subsurface
flow
constructed
wetlands."
Wat.
Res.,
35:
6(
1547­
51).

Trussel,
R.,
P.
Gagliardo,
S.
Adham,
amd
A.
Olivieri.
1998.
"
Membranes
as
an
Alternate
to
Disinfection,"
Microfiltration
II
Conference
of
the
National
Water
Research
Institute
Proceedings,
November
12
­
13,
1998,
San
Diego,
CA.

Trussell,
R.
R.
1999.
"
Safeguarding
Distribution
System
Integrity."
J.
AWWA,
91:
1:
46­
54.

Tuepker,
J.
L.,
and
C.
A.
Buescher,
Jr.
1968.
"
Operation
and
Maintenance
of
Rapid
Sand
Mixed­
Media
Filters
in
a
Lime
Softening
Plant."
J.
AWWA,
60
(
12),
1377.

United
States
Bureau
of
Reclamation.
1997.
"
Survey
of
U.
S.
Costs
and
Water
Rates
for
Desalination
and
Membrane
Softening
Plants,"
Water
Treatment
Technology
Program
Report
No.
24,
U.
S.
Bureau
of
Reclamation,
Denver,
CO.

U.
S.
Environmental
Protection
Agency.
1988.
In­
House
Pilot
Studies
for
Control
of
Chlorination
By­
Products.
Organics
Control
Branch,
Drinking
Water
Research
Division,
Risk
Reduction
Engineering
Laboratory,
Cincinnati,
OH.

U.
S.
Environmental
Protection
Agency.
1990.
Guidance
Manual
for
Compliance
with
the
Filtration
and
Disinfection
Requirements
for
Public
Water
Systems
Using
Surface
Water
Sources.
Science
and
Technology
Branch
Criteria
and
Standards
Division
Office
of
Drinking
Water.

U.
S.
Environmental
Protection
Agency.
1996.
Ultraviolet
Light
Disinfection
Technology
in
Drinking
Water
Application.
An
Overview.
EPA
811­
R­
96­
002,
EPA
Office
of
Ground
Water
and
Drinking
Water.

U.
S.
Environmental
Protection
Agency.
1998a.
Small
System
Compliance
Technology
List
for
the
Surface
Water
Treatment
Rule
and
Total
Coliform
Rule,
EPA­
815­
R­
98­
001.

U.
S.
Environmental
Protection
Agency.
1998b.
National
Primary
Drinking
Water
Regulations:
Interim
Enhanced
Surface
Water
Treatment;
Final
Rule.
Federal
Register
63(
241):
69477­
69521.
December
16,
1998.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
21
U.
S.
Environmental
Protection
Agency.
1999a.
Analysis
of
GAC
Effluent
Blending
During
the
ICR
Treatment
Studies,
EPA
815­
C­
99­
002,
EPA
Office
of
Ground
Water
and
Drinking
Water,
Technical
Support
Center.

U.
S.
Environmental
Protection
Agency.
1999b.
Alternative
Disinfectants
and
Oxidants
Guidance
Manual,
EPA
815­
R­
99­
014,
EPA
Office
of
Water.

U.
S.
Environmental
Protection
Agency.
1999c.
Enhanced
Coagulation
and
Enhanced
Precipitative
Softening
Guidance
Manual,
EPA
815­
R­
99­
012,
Office
of
Water.

U.
S.
Environmental
Protection
Agency.
2000a.
National
Primary
Drinking
Water
Regulations:
Long
Term
1
Enhanced
Surface
Water
Treatment
and
Filter
Backwash
Rule:
Proposed
Rule.
Federal
Register
65(
69):
19046­
19094.

U.
S.
Environmental
Protection
Agency.
2000b.
Stage
2
Microbial
and
Disinfection
Byproducts
Federal
Advisory
Committee
Agreement
in
Principal.
Federal
Register
65(
251):
83015.
December
29,
2000.

U.
S.
Environmental
Protection
Agency.
2001a.
Low­
Pressure
membrane
Filtration
for
Pathogen
Removal:
Application,
Implementation,
and
Regulatory
Issues,
EPA
815­
C­
01­
001,
Office
of
Water.

U.
S.
Environmental
Protection
Agency.
2001b.
National
Primary
Drinking
Water
Regulations;
Filter
Backwash
Recycling
Rule;
Final
Rule.
Federal
Register
66(
111):
31085­
31105.
June
8,
2001.

U.
S.
Environmental
Protection
Agency.
2002a.
National
Primary
Drinking
Water
Regulations:
Long
Term
1
Enhanced
Surface
Water
Treatment
and
Filter
Backwash
Rule:
FInal
Rule.
Federal
Register
67(
9):
1811­
1844.

U.
S.
Environmental
Protection
Agency.
2002b.
"
SSO
Case
Study:
Fairfax
County,
Virginia
CMOM
Program."
www.
epa.
gov/
npdes/
sso/
virginia/
index.
htm.
Last
updated
January
2002.
Downloaded
January
22,
2002.

U.
S.
Environmental
Protection
Agency.
2003.
UV
Disinfection
Guidance
Manual,
Draft,
EPA.
Office
of
Water.

Van
der
Kooij,
D.,
Hijnenk,
W.
A.
M.
and
Kruithof
J.
C.
1989.
"
The
Effects
of
Ozonation,
Biological
Filtration,
and
Distribution
on
the
Concentration
of
Easily
Assimilable
Organic
Carbon
(
AOC)
in
Drinking
Water."
Ozone
Sci.
Engr.,
11:
3:
297.

Vaughn,
J.
M.
et
al.
1987.
"
Inactivation
of
Human
and
Simian
Rotaviruses
by
Ozone."
Appl.
Env.
Microbiology
53:
2218­
2221.

Viessman,
Warren
Jr.,
and
M.
J.
Hammer.
1993.
Water
Supply
and
Pollution
Control,
Fifth
Edition,
HarperCollins
College
Publishers,
New
York,
NY.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
22
Vik,
E.
A.,
Carlson,
D.
A.,
Eikum,
A.
S.
and
Gjessing,
E.
T.
1985.
"
Removing
Aquatic
Humus
from
Norwegian
Lakes."
J.
AWWA,
77:
3:
58.

von
Sonntag,
C.
and
H­
P.
Schuchmann.
1992.
UV
disinfection
of
drinking
water
and
by­
product
formation
 
some
basic
considerations.
Journal
of
Water
Supply
Research
and
Technology
41,
No
2:
67­
74.

Vrijenhoek,
E.
M.,
A.
E.
Childress,
M.
Elimelech,
T.
S.
Tanaka
and
M.
D.
Beuhler.
1998.
"
Removing
Particles
and
THM
Precursors
by
Enhanced
Coagulation."
J.
AWWA,
90:
4:
139­
150.

Wallace,
J.
L.,
Vahadi,
B.,
Fernandes,
B.
L.
and
Boyden,
B.
H.
1988.
"
The
Combination
of
Ozone/
Hydrogen
Peroxide
and
Ozone/
UV
Radiation
for
Reduction
of
Trihalomethane
Formation
Potential
in
Surface
Water."
Ozone
Sci.
Eng.,
10:
1:
103.

Wang,
B.,
Tian,
J.,
Yin,
J.
and
Shi,
G.
1989.
"
Ammonia,
Nitrite,
and
Nitrate
Nitrogen
Removal
from
Polluted
Source
Water
with
Ozonation
and
BAC
Processes."
Ozone
Sci.
Engr.,
11:
2:
227.

Wang,
J.
Z.,
R.
Song
and
S.
A.
Hubbs.
2000.
"
Particle
removal
through
riverbank
filtration
process."
Proceedings,
Water
Quality
Technology
Conference,
November
5­
9,
2000;
Salt
Lake
City,
Utah.
American
Water
Works
Association,
Denver,
Colorado.

Wang,
J.
Z.,
R.
Song
and
S.
A.
Hubbs.
2000.
"
Particle
removal
through
riverbank
filtration
process."
Proceedings
of
International
Riverbank
Filtration
Conference,
November
2­
4,
Düsseldorf.
W.
Julich
and
J.
Schubert,
eds.,
Internationale
Arbeitgemeinschaft
der
Wasserwerke
im
Rheineinzugsgebiet,
Amsterdam,
pp.
127­
138.

Wang,
J.
Z.,
R.
S.
Summers,
R.
J.
Miltner.
1995.
"
Biofiltration
Performance
Part
1,
Relationships
to
Biomass."
J.
AWWA,
87:
12:
55.

Weber,
W.
J.
1972.
Physicochemical
Processes
for
Water
Quality
Control,
John
Wiley
&
Sons,
New
York,
NY.

Weber,
W.
J.
and
A.
M.
Jodellah.
1985.
"
Removing
Humic
Substances
by
Chemical
Treatment
and
Adsorption."
J.
AWWA,
77:(
4):
132.

Weber,
W.
J.,
Voice,
T.
C.
and
Jodellah,
A.
1983.
"
Adsorption
of
Humic
Substances:
The
Effects
of
Heterogeneity
and
System
Characteristics."
J.
AWWA,
75:
12:
612.

Werdehoff,
K.
S.
and
P.
C.
Singer.
1987.
"
Chlorine
Dioxide
Effects
on
THMFP,
TOXFP,
and
the
Formation
of
Inorganic
By­
Products,"
J.
AWWA,
79:
9:
107.

Westerhoff,
G.
and
Chowdhury,
Z.
K.
1996.
"
Water
Treatment
Systems."
Chapter
in
Water
Resources
Handbook,
L.
M.
Mays
ed.,
McGraw
Hill,
New
York.
Technologies
and
Costs
for
Control
of
Microbial
Contaminants
and
Disinfection
Byproducts
June
2003
5­
23
White
G.
C.
1999.
Handbook
of
Chlorination
and
Alternative
Disinfectants,
John
Wiley
&
Sons,
Inc.,
New
York,
NY.

White,
M.
C.,
Thompson,
J.
D.,
Harrington,
G.
W.,
and
Singer,
P.
C.
1997.
"
Evaluating
Criteria
for
Enhanced
Coagulation
Compliance."
J.
AWWA,
89:
5:
64.

Wiesner,
M,
Schroelling,
D.,
Pickering,
K.
1991.
"
Permeate
Behavior
and
Filtrate
Quality
of
Tubular
Cermanic
Membranes
Used
for
Surface
Water
Treatment."
AWWA
Membrane
Technology
Conference
Proceedings,
Orlando,
FL.

Wiesner,
M.,
Veerapaneni,
R.,
Brejchova,
D.
1992.
"
Improvements
in
Membrane
Microfiltration
Using
Coagulation
Pretreatment."
Chemical
Water
and
Wastewater
Treatment
II.
Springer­
Verlag,
New
York,
p.
281.

Wilson,
B.
R.;
P.
F.
Roessler,
E.
Van
Dellen,
M.
Abbaszadegan
and
C.
P.
Gerba.
1992.
"
Coliphage
MS­
2
as
a
UV
Water
Disinfection
Efficacy
Test
Surrogate
for
Bacterial
and
Viral
Pathogens."
Proceedings
of
1992
Water
Quality
Technology
Conference,
Nov
15­
19,
Toronto,
pp.
219.

Wood,
P.
R.,
Jackson,
D.
F.,
Gervers,
J.
A.,
Waddell,
D.
H.
and
Kaplan,
L.
1980.
Removing
Potential
Organic
Carcinogens
and
Precursors
From
Drinking
Water.
USEPA
Rpt.
No.
EPA/
600/
2­
80/
130
Cincinnati,
OH.

Wright,
H.
B
and
W.
L.
Cairns.
1998.
"
Ultraviolet
Water
Disinfection."
Technical
literature
distributed
by
Trojan
Technologies,
Inc.,
London,
Ontario,
Canada.

Wuhrmann,
K.
and
Meyrath,
J.
1955.
"
The
Bactericidal
Action
of
Ozone
Solution."
J.
Allgen.
Pathol.
Bakteriol.,
18:
1060.

Yoon,
Y.,
Amy,
G.,
Pellegrino,
J.,
Cho,
Jaeweon,
C.
1999.
"
NOM
Rejection
by,
and
Flux­
decline
of,
Nanofiltration
(
NF
and
Ultrafiltration
(
UF)
Membranes:
Scale­
up
Effects
and
Optimal
Operating
Conditions."
AWWA
Membrane
Technology
Conference
Proceedings,
Long
Beach,
CA.

Young,
J.
S.
and
Singer,
P.
C.
1979.
"
Chloroform
Formation
in
Public
Water
Supplies:
A
Case
Study."
J.
AWWA,
71:
12:
87.

Zheng,
M,
S.
A.
Andrews,
and
J.
R.
Bolton.
1999.
Impacts
of
medium
pressure
UV
on
THM
and
HAA
formation
in
pre­
UV
chlorinated
drinking
water.
Water
Quality
Technology
Conference,
October
31­
November
3,
Tampa,
FL.