EPA 832-R-95-006
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December 1995
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WASTEWATER STABILIZATION PONDS ON THE
MEXICO-USA BORDER
PERFORMANCE AND UPGRADING POTENTIAL
PREPARED FOR:
MUNICIPAL TECHNOLOGY BRANCH
OFFICE OF WATER
US ENVIRONMENTAL PROTECTION AGENCY
WASHINGTON, DC
Contract No.: 68-C2-0102
Work Assignment 2-16
December 1995
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Acknowledgements
ACKNOWLEDGEMENTS
Dr. E. Joe Middlebrooks, P.E., University of Nevada - Reno, Reno, NV, and Mr.
Sherwood Reed, P.E., Environmental Engineering Consultants, Norwich, VT
were the authors of this document. Dr. Middlebrooks conducted all of the site
visits and performed all of the data analysis and is the principal author of this
report. The work was performed under the direction of Mr. Robert E. Lee,
Chief, Municipal Technology Branch, and Mr. Robert Bastian, Work Assignment
Manager, U.S. EPA Office of Wastewater Enforcement and Compliance.
Parsons Engineering Science, Inc., Fairfax, VA provided management and
production support during the preparation of the report.
The authors would like to express their thanks to various staff members of the
International Boundary and Water Commission for their assistance. Specifically,
these include: Mr. Alton L. Goff, Project Manager of the Yuma Office of the
IBWC for his assistance on the systems at Yuma and Mexican, Baja California
Norte (BCN) and for guidance during the site visit; Mr Carlos Pena, Jr. of the
Nogales Office of IBWC and Mr. Richard L. Caldwell, Water/Wastewater
Compliance Specialist of the City of Nogales for their assistance on the Nogales
system; Mr. Enrique Reyes of the Mercedes Office of IBWC and Mr. Yusaf
Farran of the El Paso Office of IBWC for their general assistance on this project.
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Table of Contents
TABLE OF CONTENTS
ACKNOWLEDGEMENTS i
CHAPTER 1 INTRODUCTION , 1-1
SUMMARY AND CONCLUSIONS 1-2
CHAPTER 2 DESIGN OF POND SYSTEMS 2-1
PRELIMINARY TREATMENT 2-4
FACULTATIVE PONDS 2-4
Areal loading rate method 2-4
Gloyna equation 2-5
Complete-mix model 2-7
Plug flow model 2-9
Wehner Wilhelm equation 2-10
Comparison of facultative pond design models .... 2-13
PARTIAL-MIX AERATED PONDS 2-13
Partial mix design model 2-13
Selection of reaction rate constants 2-14
Temperature effects 2-14
Pond configuration . 2-15
Mixing and aeration 2-16
Example 2-17
Solution 2-17
COMPLETE MIX AERATED POND 2-22
Complete Mix Model 2-25
CONTROLLED DISCHARGE PONDS 2-25
COMPLETE RETENTION PONDS 2-27
COMBINED SYSTEMS . . . 2-28
ANAEROBIC PONDS 2-28
PATHOGEN REMOVAL 2-30
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Table of Contents
SUSPENDED SOLIDS REMOVAL 2-30
Intermittent sand filtration 2-30
Microstrainers 2-32
Rock filters 2-32
Other solids removal techniques 2-33
NITROGEN REMOVAL 2-33
Design models . 2-34
Application 2-37
PHOSPHORUS REMOVAL 2-37
Batch chemical treatment 2-37
Continuous overflow chemical treatment 2-37
PHYSICAL DESIGN AND CONSTRUCTION 2-38
Dike construction 2-39
Pond sealing 2-39
Pond hydraulics 2-40
STORAGE PONDS FOR LAND TREATMENT SYSTEMS . . 2-41
CHAPTER 3 MEXICALI, BAJA CALIFORNIA NORTE (BCN)
MEXICO WASTEWATER TREATMENT SYSTEM .3-1
SYSTEM DESCRIPTION 3-1
PERFORMANCE OF SYSTEM . . . 3-5
Design Limitations 3.5
Performance of Anaerobic Ponds 3-5
Effluent Characteristics 3-5
BOD Loadings and Loading Rates . 3-12
BOD vs Hydraulic Detention Time 3-12
BOD-Temperature 3-17
Temperature Corrected BOD and Detention Time ..3-17
PREDICTED PERFORMANCE 3-17
REDESIGN OF MEXICALI BAJA CALIFORNIA NORTE {BCN)I
SYSTEM 3_21
HI
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Table of Contents
CHAPTER 4 NOGALES INTERNATIONAL WASTEWATER TREATMENT
PLANT '. 4-1
SYSTEM DESCRIPTION . . ; .4-1
DESIGN ANALYSIS 4-3
Design Assumptions 4-3
Design Predictions 4-4
20 °C 4-5
11 °C . . . . 4-6
Oxygen Requirements 4-11
Complete Mix Cell 4-11
Partial Mix Cells 4-12
PERFORMANCE OF SYSTEM 4-12
CHAPTER 5 REYNOSA, TAMAULIPAS, MEXICO WASTEWATER TREATMENT
SYSTEM 5-1
i
CHAPTER 6 OTHER UPGRADING TECHNOLOGIES 6-1
CONSTRUCTED WETLANDS 6-1
LAND APPLICATION OF LAGOON EFFLUENT 6-2
DUCKWEED COVER . . . 6-3
SYNOPSIS OF PERFORMANCE EXPECTATIONS 6-3
REFERENCES R-1
APPENDIX A NOGALES INTERNATIONAL WASTEWATER TREATMENT
PLANT MONTHLY REPORTS
IV
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CHAPTER 1
INTRODUCTION
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Chapter 1
CHAPTER 1
INTRODUCTION
Stabilization ponds are one of the most widely used wastewater
treatment technologies. Facultative ponds have been used worldwide for over
3,000 years under the full wide range of climatic conditions. Stabilization
ponds have been in use in the USA since the early 1 900s. Today there are
approximately 7,000 pond systems in use in the USA. Variations of the basic
stabilization form of biological treatment also have been developed to attempt
to increase the loading rates, reduce detention times, decrease water loss
through evaporation and to limit discharges to surface waters. For the most
part, these variations are fully proven and widely used in many parts of the
USA and Mexico. In addition to the proven modifications, several innovative
technologies (e.g. Advanced Integrated Pond Systems, Lemna duckweed
systems and rock filters) have great potential for retrofitting basic stabilization
ponds and enhancing their performance along the US/Mexican border.
At the present time there are significant needs along the border for
effective, low cost, low maintenance, wastewater treatment concepts. Pond
systems, either new facilities or upgrading existing ponds, offer the potential
for resolution of these needs in many locations.
Under Contract No. 68-C2-0102, Work Assignment 2-16, Parsons
Engineering Science, Inc. (Parsons ES) in conjunction with E. Joe Middlebrooks
and Sherwood C. Reed of Environmental Engineering Consultants of Norwich,
Vermont has been requested to provide an evaluation of the use of pond
systems for treating wastewater along the US/Mexican border. The objective
of this work assignment is to provide useful information and guidance for
planners and engineers for use in considering the potential application of pond
systems and in preparing preliminary project designs for application along the
US/Mexican border area.
1-1
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Chapter 1
SUMMARY AND CONCLUSIONS
1. The wastewater stabilization ponds evaluated along the Mexican-USA
border were not constructed as designed (i.e., aeration omitted).
Consequently the systems are not performing at a satisfactory level;
however, all of the systems visited appear to be upgradable to efficient
and reliable facilities.
2. By converting the systems to combinations of complete and partial mix
aerated lagoons, the systems can:be expected to produce effluent BOD
concentrations of less than 10 mg/l and process two to three times the
current flow rate. •
3. Installing multiple outlets and multiple drawoff depths in the final cells
of all three systems would materially improve the effluent TSS quality.
4. Improvements in the hydraulic characteristics of the lagoon systems
would have a significant impact on performance.
5. Regardless of the modifications made to the systems, to achieve the
maximum efficiency from the lagoon systems it is essential that proper
operation be provided. For example, it will do little good if multiple
depth drawoff outlets are installed but not used.
6. Existing wastewater stabilization lagoons can be economically upgraded
to produce an effluent of practically any quality desired by the utilization
of many processes, many of which are briefly discussed in Chapter 2.
Design of Pond Systems (intermittent sand filtration, rock filters,
microstrainers, dissolved air flotation, centrifugation, etc.).
7. In addition to the upgrade methods referred to above, wetlands,
duckweed, and land treatment appear to be viable upgrade alternatives
for lagoon effluents, but additional study is needed to confirm their
viability.
8. Two of three systems (Mexicalj, Baja California Norte (BCN), and
Reynosa) visited are grossly overlpaded, but in view of the operational
effort and inadequate design, the;systems perform remarkably well.
1-2
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Chapter 1
9. The Nogales system is relatively new, well operated, and produces an
excellent quality effluent. Relatively simple modifications in the lagoon
system would double or triple the flow rate that could be processed by
the lagoon system. Modifications in the solids removal activities would
be necessary if higher flow rates are to be processed by the facility.
10. Less than optimal solids removal processes have been employed at the
Nogales facility, and modifications are needed to maximize the efficiency
of the units.
11. At the Nogales facility, reductions in the hydraulic residence time in the
final settling cells probably would reduce the algae load going to the
automatic backwash filters. Normal granular media filtration has been
shown to be capable of removing only one-third of the solids in lagoon
effluents without chemical addition. Consideration should be given to
some type addition to improve the filter efficiency.
1-3
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CHAPTER 2
DESIGN OF POND SYSTEMS
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Chapter 2
CHAPTER 2
DESIGN OF POND SYSTEMS
Stabilization ponds have been employed for treatment of wastewater for
over 3000 years. The first recorded construction of a pond system in the
United States was at San Antonio, TX, in 1901. Today, over 7000 pond
systems are used in the U.S. for the treatment of municipal and industrial
wastewaters (USEPA, 1980), under a wide range of weather conditions ranging
from tropical to Arctic. Large numbers of pond systems are used throughout
the world (WHO, 1987). Many types of pond systems are utilized on both
sides along the border between Mexico and the USA. Three pond systems
located along the Mexico-USA border were visited and evaluated. The results
of these evaluations are presented in Part II. Pond systems in Mexicali BCN and
Reynosa, Mexico, and Nogales, Arizona, USA were visited. These pond
systems -are used alone or in combination with other wastewater treatment
processes.
Wastewater pond systems can be classified by dominant type of
biological reaction, duration and frequency of discharge, extent of treatment
ahead of the pond, or arrangement among cells (if more than one cell is used).
The most basic classification depends on the dominant biological reactions
occurring in the pond, and the four principal types are:
o Facultative (aerobic-anaerobic) ponds
o Aerated ponds (Complete and Partial Mix)
p Aerobic Ponds
o Anaerobic ponds
All four types depend on the interaction of the in-situ biological
components for treatment and can be considered to be "natural treatment
systems." General design features and performance expectations for pond
systems and a modification of pond systems using water hyacinths are
presented in Table 2-1.
The most common type is the facultative pond. Other terms which are
commonly applied are oxidation pond, sewage lagoon, and photosynthetic
pond. Facultative ponds are usually 1.2 to 2.5 m (4 to 8 ft) in depth, with an
aerobic layer overlying an anaerobic layer, often containing sludge deposits.
The usual detention time is 5 to 30 days. Anaerobic fermentation occurs in the
lower layer and aerobic stabilization occurs in the upper layer. The key to
facultative operation is oxygen production by photosynthetic algae and surface
reaeration. The oxygen is utilized by the aerobic bacteria in stabilizing the
2-1
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Chapter 2
organic material in the upper layer. The algae are necessary for oxygen
production, but their presence in the final effluent represents one of the most
serious performance problems associated with facultative ponds.
The total containment pond and the controlled discharge pond are forms
of facultative ponds. The total containment pond is applicable in climates
where the evaporative losses exceed the rainfall. Controlled discharge ponds
have long detention times, and the effluent is discharged once or twice per year
when the effluent quality and stream conditions are satisfactory. A variation
of the controlled discharge pond, used in the southern U.S. is called a
hydrograph controlled release lagoon. The pond discharge is matched to
periods of high flow in the receiving stream, using the stream hydrograph as
the control.
In an aerated pond, oxygen is supplied mainly through mechanical or
diffused aeration. Aerated ponds are generally 2 to 6 m (6 to 20 ft) in depth
with detention times of 3 to 10 days. The chief advantage of aerated ponds
is that they require less land area. Aerated ponds can be designed as complete
mix reactors or as partial mix reactors. In the former case sufficient energy
must be used to keep the pond contents in suspension at all times. The basic
design of a complete mix reactor is similar to that of an activated sludge
system without sludge recycle.
Aerobic ponds, also called high rate aerobic ponds, maintain dissolved
oxygen (DO) throughout their entire depth. They are usually 30 to 45 cm (12
to 18 in) deep, allowing light to penetrate the full depth. Mixing is often
provided to expose all algae to sunlight and to prevent deposition and
subsequent anaerobic conditions. Oxygen is provided by photosynthesis and
surface reaeration, and aerobic bacteria stabilize the waste. Detention time is
short, three to five days being usual. Aerobic ponds are limited to warm sunny
climates and are used infrequently in the United States.
Anaerobic ponds receive such a heavy organic loading that there is no
aerobic zone. They are usually 2.5 to 5 m (8 to 15 ft) in depth and have
detention times of 1 to 50 days depending upon the environment in which they
function. The principal biological reactions occurring are acid formation and
methane fermentation. Anaerobic ponds are usually used for treatment of
strong industrial and agricultural wastes, or as a pretreatment step where an
industry is a significant contributor to a municipal system. They do not have
wide application to the treatment of municipal wastewater in the USA, but are
used successfully in many areas of the world.
2-3
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Chapter 2
PRELIMINARY TREATMENT
In general, the only mechanical or monitoring and control equipment
required for wastewater pond systems are flow measurement devices, sampling
systems, and pumps. Design criteria and examples for preliminary treatment
components can be found in a number of references, as well as in equipment
manufacturer's catalogs (AI-Layla et al., 1980; Metcalf and Eddy, 1991; Ten
State Standards, 1978; Wallace, 1978; and Water Pollution Control Federation,
1 977). Flow measurement can be accomplished with relatively simple devices
such as Palmer-Bowlus flumes, V-notch weirs, and Parshall flumes used in
conjunction with a recording meter. Frequently, flow measurements and 24-
hour compositing samplers are combined in a common manhole, pipe, or other
housing arrangement. If pumping facilities are necessary, the wet well is
sometimes used as a point to recycle effluent or to add chemicals for odor
control. Pretreatment facilities should be kept to a minimum at pond systems.
FACULTATIVE PONDS
Facultative pond design is based upon BOD removal; however, the
majority of the suspended solids will be removed in the primary cell of append
system. Sludge fermentation feedback of organic compounds to the water in
a pond system is significant and has an effect on the performance. During the
spring and fall, the thermal overturn of the pond contents can result in
significant quantities of benthic solids being resuspended. The rate of sludge
accumulation is affected by the liquid temperature, and additional volume is
added for sludge accumulation in cold climates. Although SS have a profound
influence on performance of pond systems, most design equations simplify the
incorporation of the influence of SS by using an overall reaction rate constant.
Effluent SS generally consist of suspended organism biomass and do not
include suspended waste organic matter,
Several empirical and rational models for the design of these ponds have
been developed. These include the ideal plug flow and complete mix models,
as well as models proposed by Fritz, et al. (1979); Gloyna (1971); Larson
(1974), Marais(1970); McGarry and Pescod (1970), Oswald etal. (1970); and
Thirumurthi (1974). Several produce satisfactory results, but the use of some
may be limited because of the difficulty in evaluating coefficients or by the
complexity of the model.
Areal loading rate method
Canter and Englande (1970) reported that most states have design
criteria for organic loading and/or hydraulic detention time for facultative ponds.
2-4
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Chapter 2
These criteria are assumed to ensure satisfactory performance; however,
repeated violations of effluent standards by pond systems that meet state
design criteria indicate the inadequacy of the criteria. A summary of the state
design criteria for each location and actual design values for organic loading and
hydraulic detention time for four facultative pond systems evaluated by the
Environmental Protection Agency (Middlebrooks, 1987 and USEPA, 1981) are
shown in Table 2-2. Also included is a list of the months the federal effluent
standards for BOD5 were exceeded. The actual organic loading for the four
systems is nearly equal, but the system in Corinne, UT consistently satisfied
the federal effluent standard. This may be a function of the larger number of
cells in the Corinne system; seven as compared to three for the others. More
hydraulic short-circuiting is likely to occur in the three cell systems, resulting
in an actual detention time which was shorter than exists in the Corinne
system. The detention time may also be affected by the location of the pond
cell inlet and outlet structures.
Based on many years of experience, the following loading rates for
various climatic conditions are recommended for use in designing facultative
pond systems. For average winter air temperatures above 15°C (59°F), a BOD5
loading rate range of 45 to 90 kg/ha-d (40-80 Ib/ac-d) is recommended. When
the average winter air temperature ranges between 0° and 1 5°C (32° to 59°F)
the organic loading rate should range between 22 and 45 kg/ha-d (20-40 Ib/ac-
d). For average winter temperatures below 0°C (32°F) the organic loading
should range from 11 to 22 kg/ha-d (10-20 Ib/ac-d).
The BOD loading rate in the first cell is usually limited to 40 kg/ha-d (35
Ib/ac/d) or less, and the total hydraulic detention time in the system is 1 20 to
180 days in climates where the average air temperature is below 0°C (32°F).
In mild climates where the air temperature is greater than 15°C (59°F), loadings
on the primary cell can be 100 kg/ha-d (89 Ib/ac-d).
Gloyna equation
Gloyna (1971) has proposed the following empirical equation for the
design of facultative wastewater stabilization ponds:
V = (3.5 x 10-5)(Q)(La)[0(35-Tl](f)(f) (1)
where V = pond volume, m3
Q = influent flow rate, L/d.
La = ultimate influent BOD or COD, mg/l
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Chapter 2
6 = temperature correction coefficient = 1.085
T = pond temperature, °C.
f = algal toxicity factor.
f = sulfide oxygen demand.
The BOD5 removal efficiency is projected to be 80 to 90 percent based
on unfiltered influent samples and filtered effluent samples. A pond depth of
1.5 m (5 ft) is suggested for systems with significant seasonal variations in
temperature and major fluctuations in daily flow. The surface area design using
Eq. 1 should always be based on a 1 m (3 ft) depth. The algal toxicity factor
(f) is assumed to be equal to 1.0 for domestic wastes and many industrial
wastes. The sulfide oxygen demand (f')is also equal to 1.0 for sulfate
equivalent ion concentration of less than 500 mg/l. The design temperature is
usually selected as the average pond temperature in the coldest month.
Sunlight is not considered to be critical in pond design, but can be incorporated
into Eq. T by multiplying the pond volume by the ratio of sunlight at the design
location to the average found in the southwestern United States.
The Gloyna method was evaluated using the data referenced in Table
2-2. The equation giving the best fit of the data is shown below as Eq. 2.
There was considerable scatter to the data, but the relationship is statistically
significant.
V = 0.035Q(BOD)C\.09Q)UGHT{3^-TI/250
(2)
where BOD = BOD5 in the system influent, mg/l.
LIGHT = solar radiation in langleys.
V = pond volume, m3
Q = influent flow rate, m3/day
T = pond temperature, °C
Complete-mix model
The Marias & Shaw (1961) equation is based on a complete mix-
model and first order kinetics. The basic relationship is shown in Eq. 3.
2-7
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Chapter 2
$L- T— L_l"
c0 n+t
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Chapter 2
Plug flow model
The basic equation for the plug-flow model is:
-^ = exp [-kpt]
(6)
where Ce = effluent BOD5 concentration, mg/l.
C0 = influent BOD5 concentration, mg/l.
kp = plug flow first order reaction rate, days"1
t = hydraulic residence time, days
The reaction rate (kp) varies with the BOD loading rate as shown in Table
2-3.
Table 2-3
Variation of the Plug-Flow Reaction Rate Constant with
Organic Loading Rate {Neel et al., 1961)
Organic Loading Rate
kg/ha-daya . kpb, days'1
22 0.045
45 0.071
67 0.083
90 0.096
112 0.129
a kg/ha-d x 0.8907 = Ib/ac-d.
b reaction rate constant at 20°C.
The influence of water temperature on the reaction rate constant can be
determined with Eq. 6a.
(6a)
2-9
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Chapter 2;
where kpT = reaction rate at temperature T, days"1
kp20 = reaction rate at 20°C, days"1
T = operating water temperature, °C.
Wehner Wilhelm equation
Thirumurthi (1974) found that the flow pattern in facultative ponds is
somewhere between ideal plug-flow and complete-mix, and he
recommended the use of the following chemical reactor equation developed
by Wehner and Wilhelm (1956) for chemical reactor design. ;
CM 1 /if)n\
A op i I\£L))
(7)
where C0 = influent BOD concentration, mg/l
Ce = effluent BOD concentration, mg/l
e = base of natural logarithms, 2.7183
a = (1 + 4ktD)a5 I
k = 1st order reaction rate constant, days"1
t = hydraulic residence time, days
D = dimensionless dispersion number
= H/vL = Ht/L2
H = axial dispersion coefficient, area per unit time
v = fluid velocity, length per unit time
L = length of travel path of a typical particle
Thirumurthi (1974) prepared the chart shown in Fig.2-1 to facilitate the
use of Eq.7. The dimensionless term kt is plotted versus the percentage of
BOD remaining for dispersion numbers ranging from zero for an ideal plug flow
2-10
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Chapter 2
o
O)
6 8 10 15 20 30 O) 50 50
BOD Remaining (percent)
FIGURE 2-1 WEHIMER AND WILHELM EQUATION CHART (THIRUMURTHI, 1974).
2-11
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Chapter 2
unit to infinity for a completely mixed unit. Dispersion numbers measured in
wastewater ponds range from 0.1 to 2.0 with most values less than 1 .0., The
selection of a value for D can dramatically affect the detention time required to
produce a given quality effluent. The selection of a design value for k can have
an equal effect. If the chart in Fig. 2-1 is not used, Eq. 7 can be solved on a
trial and error basis. i
To improve on the selection of a D; value for use in Eq. 7, Polprasert
and Bhattarai (1985) developed Eq. 8 based on data from pilot and full scale
pond systems.
(8)
where D = dimensionless dispersion number
t = hydraulic residence time, days
v = kinematic viscosity, m2/day
d = liquid depth of pond, m
W = width of pond, m
L = length of pond, m
The hydraulic residence time used to derive Eq. 8 was determined by
tracer studies; therefore, it is still difficult to estimate the value of D to use
in Eq. 7. A good approximation is to assume that the actual hydraulic |
residence time is half that of the theoretical hydraulic residence time.
The variation of the reaction rate constant k in Eq. 7 with the water
temperature is determined with Eq. 9.
where kT = reaction rate at water temperature T, days"1
k20 = reaction rate at 20°C = 0.15 days'1
T = operating water temperature, °C
2-12
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Chapter 2
Comparison of facultative pond design models
Because of the many approaches to the design of facultative ponds it is
not possible to recommend the "best" procedure. An evaluation of the design
methods presented above, with operational data referenced in Table 2-2, failed
to show that any of the models are superior to the others in terms of predicting
the performance of facultative pond systems (Middlebrooks et al., 1978;
USEPA, 1981; and Reed et al., 1995).
PARTIAL-MIX AERATED PONDS
In the partial mix aerated pond system the aeration serves only to provide
an adequate oxygen supply, and there is no attempt to keep all of the solids in
suspension in the pond as is done with complete mix and activated sludge
systems. Some mixing obviously occurs and keeps portions of the solids
suspended; however, an anaerobic degradation of the organic matter that
settles does occur. The system is sometimes referred to as a facultative
aerated pond system.
Even though the pond is only partially mixed, it is conventional to estimate
the BOD removal using a complete mix model and first order reaction kinetics.
Recent studies (Middlebrooks, 1987) have shown that a plug flow model and
first order kinetics more closely predict the performance of these ponds when
either surface or diffused aeration is used. However, most of the ponds
evaluated in this study were lightly loaded and the reaction rates calculated are
very conservative because the rate decreases as the organic loading decreases
(Neel et al., 1961). Because of the lack of better design reaction rates, it is still
necessary to design partial mix ponds using complete mix kinetics.
Partial mix design model
The design model using first order kinetics and operating "n" number of
equal sized cells in series is given by Eq. 10.
(10)
where Cn = effluent BOD concentration in cell n, mg/l
C0 = influent BOD concentration, mg/l
k = first order reaction rate constant, days"1
2-13
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Chapter 2
= 0.276 day"1 at 20°C (assumed to be constant in all cells).
t = total hydraulic residence time in pond system, days
n = number of cells in the series.
If other than a series of equal volume ponds are to be employed, it is
necessary to use the following general equation: ;
(11)
where k1; k2/...kn are the reaction rates in cells 1 through n (all usually assumed
equal for lack of better information) and t,, t2,...tn are the hydraulic residence
times in the respective cells.
It has been shown (Mara, 1975) that a number of equal volume reactors
in series is more efficient than unequal volumes; however, due to site
topography or other factors there may be cases where it is necessary to
construct cells of unequal volume.
Selection of reaction rate constants. The selection of the k value is the critical
decision in the design of any pond system. A design value of 0.276 day'1 is
recommended by the Ten States Standards (1978) at 20°C and 0.138 day"1 at
1°C. Using these values to calculate the temperature coefficient yields a value
of 1.036. Boulier and Atchinson (1975) recommended values of k of 0.2 to
0.3 at 20°C and 0.1 to 0.15 at 0.5°C. A temperature coefficient of 1.036
results when the two lower or higher values of k are used in the calculation.
Reid (1970) suggested a k value of 0.28 at 20°C and 0.14 at 0.5°C based on
research with partial mix ponds aerated with perforated tubing in central
Alaska. These values are essentially identical to the Ten States Standards
recommendations.
Temperature effects. The influence of temperature on the reaction rate is
defined by Eq. 13.
If - If oTw-2Q
KT - A-20y (13)
2-14
-------
Chapter 2
where kT = reaction rate at temperature T, days"1
k20 = reaction rate at 20°C, days"1
© = temperature coefficient
= 1.036
Tw = temperature of pond water, °C.
The pond water temperature (Tw) can be estimated using the following
equation developed by Mancini and Barnhart (1976).
AfT.+QT,
»—Af*r l (14r
where Tw = pond water temperature, °C
Ta = ambient air temperature, °C
A = surface area of pond, m2
f = proportionality factor = 0.5.
Q == wastewater flow rate, m3/day
An-estimate of the surface area is made based on Eq.12, corrected for
temperature, and then the temperature is calculated using Eq. 14. After several
iterations, when the water temperature used to correct the reaction rate
coefficient agrees with the value calculated with Eq. 14, the selection of the
detention time in the system is completed.
Pond configuration
The ideal configuration of a pond designed on the basis of complete
mix hydraulics is a circular or a square pond; however, even though partial
mix ponds are designed using the complete mix model, it is recommended
that the cells be configured with a length to width ratio of 3:1 or 4:1. This is
done because it is recognized that the hydraulic flow pattern in partial-mix
systems more closely resembles the plug-flow condition. The dimensions of
the cells can be calculated by Eq.15.
2-15
-------
Chapter 2
V=[L W+(L -2sd) (W-2sd) +4(1 -scf) (W-sd) ] !L
6
where V = volume of pond or cell, m3 (ft3).
(15)
L = length of pond or cell at water surface, m (ft).
W = width of pond or cell at water surface, m (ft).
s = slope factor (i.e.; 3:1 slope, s = 3)
d = depth of pond, m (ft).
Mixing and aeration
In most municipal systems, the oxygen requirements control the power
input required for partial mix pond systems. A complete-mix system can
require approximately ten times the power as a system designed to satisfy the
oxygen requirements only. There are several rational equations available to
estimate the oxygen requirements for pond systems (AI-Layla et al., 1980;
Benefield and Randall, 1980; Gloyna, 1976; and Metcalf and Eddy, 1991;). In
most cases partial mix system design is based on the BOD entering the system
to estimate the biological oxygen requirements. After calculating the required
rate of oxygen transfer, equipment manufacturers' catalogs should be used to
determine the zone of complete oxygen dispersion by surface, helical, or air gun
aerators or the proper spacing of perforated tubing. Equation 16 is used to
estimate oxygen transfer rates.
N.
g[Csc C'11-025rw"20
(16)
where N = equivalent oxygen transfer to tap water at standard conditions, kg/hr
Na = oxygen required to treat the wastewater, kg/hr (usually taken as 1.5 x
the organic loading entering the cell)
a = (oxygen transfer in wastewater)/(oxygen transfer in tap water) = 0.9
CL = minimum DO concentration to be maintained in the wastewater,
assume 2 mg/l
2-16
-------
Chapter 2
Cs = oxygen saturation value of tap water at 20°C and one atmosphere
pressure
= 9.17 mg/l.
Tw = wastewater temperature, °C.
Csw =& (CSS)P = oxygen saturation value of the. waste, mg/l.
0 = {wastewater saturation value)/tap water oxygen saturation value) = 0.9
Css = tap water oxygen saturation value at temperature Tw, {see oxygen
saturation tables in Standard Methods or many textbooks).
P = ratio of barometric pressure at the pond site to barometric pressure at
sea level, {assume 1.0 for an elevation of 100 m)
Eq. 14 can be used to estimate the water temperature in the pond during
the summer months which will be the critical period for design. The use of the
partial-mix design procedure is illustrated by the following example.
Example. Design a four cell partial-mix aerated pond for the following
environmental conditions and wastewater characteristics. Q = 151,400
m3/day, C0 = 300 mg/l, Ce from fourth cell = 30 mg/l, k20 = 0.276 day'1,
winter air temperature = 10°C, summer air temperature = 40°C, influent water
temperature = 15 °C, elevation = 100 m, maintain a minimum DO
concentration of 2 mg/l in all cells, use a pond depth of 4 m.
Solution
1. Assume a winter pond water temperature of 10°C and calculate the volume
of a cell in the pond system.
k = (0.276)(1.036)(1°-20) = 0.194 day1
r=
4
0.194
300]
30 j
= 16.0 days
= 4.0 days
V, = {4.0)(151,400 m3/day) = 605,600 m3, use three trains, V^ = 202,867 m3
2-17
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Chapter 2
2. Assuming that the pond cells have a length to width ratio of 4: 1 , calculate
the dimensions of the cell using Eq. 15.
V .2 = 4W x W+(4W-2x3x4)(W-2x3x4)+4(4W-3x4)(W-3x4)
1.5V = 24W2-360W +1152
or: W2- 15W = (1.5/24MV) - 48 - 0.0625(202,867) - 48 = 12,631
Solve the quadratic equation by completing the square:
W2- 15W + 56.25 = 12,631 + 5.6.25 !
(W- 7.5)2 = 12,687.25
W- 7.5 = 112.6
W = 120.1 m
L = (120.1K4) = 480.4 m \
Surface Area A = (120.1)(480.4) = 57,696 m2
3. Check the pond temperature using the calculated cell area of 57,696 m2
and the other known characteristics in Eq. 14.
= Xlfr,+Q7/=(57,696)(0.5)(10)H-(50,467)(15)=13 2°C
w Af+Q (57,696)(0.5)+50,467
A temperature of 10°C was assumed, so another iteration is necessary.
4. For the second iteration assume 14°C.
k = (0.276X1.036)(14'20) = 0.223 days'1
Using Eq. 12, the total detention time for the four cell system is 14.0
days, or 3.5 days/cell.
V, = (3.5)(151,400) = 529,900 m3-^ = 176,633 rn3 '.
W2- 15W = 0.0625V-48
2-18
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Chapter 2
(W- 7.5)2'- 10,992
W = 112.3 m
L = (112.3)(4) = 449.2 m
A = (112.3) (449.2) = 50,445 m2
j =(50,445)(0.5)(14)-t-(50,467)(15)_1/l Jor
(50,445)(0.5)+50,467
This is close enough to the assumed value of 14°C; therefore, adopt the
detention time and cell dimensions calculated in this iteration. Add a freeboard
allowance of 0.6 m. This will increase the cell dimensions at the top of the
inside of the dike to 115.9m by 449.2 m. Using only 2 cells instead of 4 will
increase the detention time by about 50 percent and increase the surface area
and volume by a factor of about 3. This would be undesirable-in cold climates
because of the enhanced potential for ice formation and in all locations because
of the additional costs for construction.
5. Determine the oxygen requirements for this pond system based on the
organic loading in each cell and by using Eq. 16. The maximum oxygen
requirements will occur in the summer months.
Use Eq. 14 to estimate pond temperatures
7- J50,445)(0.5)(40)+(50,467)(15)_0.3 oor
w (50,445)(0.5)+50,467 ~
At 23°C the tap water oxygen saturation value (Css) is 8.68 mg/l (see
tables in Standard Methods or standard text books for other values).
The organic load in the influent wastewater is:
(C0)(Q) = (300g/m3)(50,467m3/day)(day/24hr)(kg/1000g) = 631 kg/h
kp = 0.276 (1.036)23-20 = 0.307
2-19
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Chapter 2
The effluent BOD from the first cell can be calculated with Eq. 10.
ci_ 1 _ 1
C0 rkt I1 (0.3Q7)(3.5)
EH'
= 0.482
C1 = 300(0.482) = 145 mg/l
Therefore the organic loading on the second cell is:
145 mg/l(50,467 m3/d)( 1000 L/m3)(1d/24 h)(1 kg/1000g)(1 g/1000mg) = 305 kg/h
Similarly,
BOD in cell 2 effluent = 70 mg/l
Organic loading on cell 3 = 147 kg/hr
BOD in cell 3 effluent = 34 mg/l
Organic loading on cell 4 = 71 kg/hr
The oxygen demand is assumed to be 1.5 times the organic loading, hence
Na1 = (1.5)(631 kg/hr) = 947 kg/h
Similarly, Na2 = 458 kg/hr, Na3 = 221 kg/hr, Na4 = 107 kg/hr. Use Eq. 16 to
calculate equivalent oxygen transfer.
N- »•
JCSW CA
L c*
,.-20
Csw = (/3}{CSS)(P) = {0.9X8.68 mg/l)(1.0) = 7.81 mg/l
A/,= _ - = -\542kgfh of O2
0 9f7.81-2.0|(1 ,025)23-20
2-20
-------
Chapter 2
Similarly,
N2 = 746 kg/h of O2
N3 = 360 kg /h of O2
N4 = 174 kg/h of 02
6. Evaluate both surface and diffused air aeration equipment. A value of 1.9
kg O2/kWh (1.4kg/hp/h) is recommended for estimating power requirements for
surface aerators. A value of 2.7 kg 02/kWh (2 kg/hp/h) is recommended by the
manufacturers of this equipment. The gas transfer rate must be verified for the
equipment selected.
The total power for surface aeration is:
Cell 1: (1542 kg/h of 02}/(1.9 kg/kWh of 02) = 812 kW (1,089 hp)
Similarly,
Cell 2: 393 kW (527 hp)
Cell 3: 189 kW (253 hp)
Cell 4: 92 kW (123 hp)
The total power for diffused aeration is:
Cell 1: (1542 kg/h of O2)/(2.7 kg/kWh of O2) = 571 kW (766 hp)
Similarly
Cell 2 = 276 kW ( 370 hp)
Cell 3 = 133 kW (178 hp)
Cell 4 = 64 kW (86 hp)
These surface or diffused aerator power requirements must be corrected for
gearing and blower efficiency. Assuming 90 percent efficiency for both gearing
and blowers, the total power for surface aerators in cell 1 would be 812 kW/
0.9 = 902 kW (1210 hp). The total power needs are about 1,651 kW for the
surface aerators and" 1,160 kW for the diffused aerators. These are
approximate values and are used for the preliminary selection of aeration
2-21
-------
Chapter 2
equipment. The actual power requirement using surface aeration will be
determined by using the zone of complete oxygen dispersion reported by the
equipment manufacturers along with the calculated power estimates. The
distribution of the two types of aeration equipment are illustrated in Figs. 2-2
and 2-3. Surface aeration equipment is subjected to potential icing problems
in cold climates, and use of the fine bubble perforated tubing requires that a
diligent maintenance program be established. A number of communities have
experienced clogging of the perforations, particularly in hard water areas.
Corrective action requires purging with HCI gas. :
The final element recommended in this partial-mix aerated pond system
is a settling cell with a 2-day detention time.
COMPLETE MIX AERATED PONDS ,
Complete mix aerated ponds are designed and operated as flow-through
ponds with or without solids recycle. Most systems are operated without solids
recycle; however, many systems are built with the option to recycle effluent
and solids. Even though the recycle option may not be exercised, it is desirable
to include it in the design to provide flexibility in the operation of the system.
If the solids are returned to the pond, the process becomes a modified activated
sludge process.
Solids in the complete mix aerated pond are kept suspended at all times.
The effluent from the aeration tank will contain from one-third to one-half the
concentration of the influent BOD in the form of solids These solids must be
removed by settling before discharging the effluent. Settling is an integral part
of the aerated pond system. Either a settling basin or a quiescent portion of
one of the cells separated by baffles may be used for solids removal.
Six factors are considered in the design of an aerated pond: 1) BOD
removal, 2) effluent characteristics, 3) oxygen requirements 4) mixing
requirements, 5) temperature effects, and 6) solids separation (Metcalf and
Eddy, 1991). BOD removal and the effluent characteristics are generally
estimated using a complete mix hydraulic model and first order reaction
kinetics. A combination of Monod-type kinetics, first order kinetics, and a
complete mix model has been proposed, but there is limited experience with the
method (Metcalf and Eddy, 1991; and Benefield and Randall, 1980). Oxygen
requirements will be estimated using equations based upon mass balances;
however, in a complete mix system the power input necessary to keep the
solids suspended is much greater than that required to transfer adequate
oxygen (Malina et al., 1972). Temperature effects are incorporated into the
BOD removal equations. Solids removal will be accomplished by installing a
2-22
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Chapter 2
'Blower House
Air Dislributicn Manifold
INFLUENT
1.5m
EFFLUENT
12m
FIGURE 2-2 LAYOUT OF AERATION SYSTEM FOR PARTIAL MIX DIFFUSED AIR
AERATED POND SYSTEM.
2-23
-------
Chapter 2
Zones of complete
oxygen dispersion
Zones of complete mixing
where solids suspension
occurs
^ Location of aerators
7 varied to prevent
channel of flow
Influent
FIGURE 2-3 LAYOUT OF SURFACE AERATORS IN FIRST CELL. OF PARTIAL
MIX SYSTEM.
2-24
-------
Chapter 2
settling pond with a two day detention time. If a higher quality effluent is
required, the solids removal devices described herein should be evaluated and
one selected to produce an acceptable effluent quality.
Complete Mix Model
The complete mix model using first order kinetics and operating in a
series with n equal volume ponds is the same as Equation 10 used for the
partial mix pond system. The differences in using Equation 10 with complete
mix systems is the change in kc (becomes 2.0 per day) and 6 in Equation 13
(becomes 1.085) .
Cn _ 1
C
0
where Cn = effluent BOD concentration in cell n, mg/l
C0 = influent BOD concentration, mg/l
k = first order reaction rate constant, days"1
— 2.0 day"1 at 20°C (assumed to be constant in all cells).
t = total hydraulic residence time in pond system, days
n = number of cells in the series.
The design example shown for a partial mix aerated lagoon can be
followed to design a complete mix system by substituting the values of kc and
6 mentioned above.
CONTROLLED DISCHARGE PONDS
No rational or empirical design model exists specifically for the design of
controlled discharge wastewater ponds as utilized in the northern U.S. and
Canada. However, the facultative pond design models may also be applied to
the design of controlled discharge ponds provided allowance is made for the
required larger storage volumes. The plug-flow model for facultative ponds can
be applied to the controlled discharge type if the hydraulic residence time is less
than 1 20 days. A study of 49 controlled discharge ponds in Michigan indicated
that residence times were 120 days or greater and discharge periods ranged
from 5 days to 30 days for each occurrence. Ponds of this type have been
2-25
-------
Chapter 2
successfully operated in the north central United States using the following
criteria:
• Overall organic loading: 22-28 kg BOD/ha-day (20-25 Ib BOD/ac-day).
• Liquid depth: not more than 2 m (6 ft) in first cell, not more than 2.5 m
(8 ft)in subsequent cells.
• Hydraulic detention: at least 6 months storage above the 0.6 m (2 ft)
liquid level (including precipitation), but not less than the period of ice
cover.
• Number of cells: at least 3 for reliability, with interconnected piping for
parallel or series operation.
The design of the controlled discharge pond must include an analysis
showing that receiving stream water quality standards will be maintained during
the discharge period, and that the receiving watercourses can accommodate
the discharge rate from the pond. The design must also develop a
recommended discharge schedule.
Selecting the optimum day and hour for release of the pond contents is
critical to the success of this method. The operation and maintenance manual
must include instructions on how to correlate pond discharge with effluent and
stream quality. The pond contents and stream must be carefully examined,
before and during the discharge period.
• The following steps are usually taken for discharge from all systems:
• Isolate the cell to be discharged, usually the final one in series, by
valving off the inlet line from the preceding cell.
• Analyze cell contents for parameters of concern in the discharge permit.
• Plan activities to spend full time on control of discharge during the
entire discharge period.
• Monitor conditions in receiving stream and request approval from
regulatory agency for discharge.
• Commence discharge when approval is received and continue as long
as weather is favorable, and dissolved oxygen levels and turbidity are
below limits. Typically the last two cells in the series are sequentially
2-26
-------
Chapter 2
isolated and drawn down. Then discharge is interrupted for a week or
more while raw wastewater is diverted to one of the cells which has been
drawn down. The purpose here is to isolate the first cell prior to its
discharge. When the first cell is drawn down to about 60 cm (24 in)
depth, the usual internal series flow pattern, without discharge is
resumed.
• During the discharge periods, samples are taken at least three times
daily near the discharge pipe for immediate dissolved oxygen analysis.
Additional testing may be required for SS and other parameters.
Experience with the operational concept listed above is limited to northern
states with seasonal and climatic constraints on performance. A continuous
ice cover on a facultative pond will lower performance and little better than
primary effluent will result if discharge is permitted during such periods.
Stringent limits on SS may also limit discharge during the seasonal algal bloom
periods. The concept will be quite effective for BOD removal in any location.
The process will also work with a more frequent than semi-annual discharge
cycle, depending on receiving water conditions and requirements.
The hydrograph-controlled release (HCR) pond is a variation of this
concept, which was developed for use in the southern United States, but can
be effectively used in most areas of the country. In this case the discharge
periods are controlled by a gauging station in the receiving stream and are
allowed to occur during high flow periods. During low flow periods the effluent
is stored in the HCR pond. The process design uses conventional facultative
or aerated ponds for the basic treatment, followed by the HCR cell for
storage/discharge. No treatment allowances are made during design for the
residence time in the HCR cell; its sole function is storage. Depending on
stream flow conditions, the storage needs may range from 30 to 120 days.
The design maximum water level in the HCR cell is typically about 2.4 m (8 ft)
with the minimum water level at 0.6 m (2 ft). Other physical elements are
similar to conventional pond systems. The major advantage for HCR systems
is the possibility of utilizing lower discharge standards during high flow
conditions as compared to a system designed for very stringent low flow
requirements and then operated in that mode on a continuous basis.
COMPLETE RETENTION PONDS
In areas of the world where the moisture deficit, evaporation minus
rainfall, exceeds 75 cm (30 in) annually, a complete retention wastewater pond
may prove to be the most economical method of disposal if low cost land is
available. The pond must be sized to provide the necessary surface area to
2-27
-------
Chapter 2
evaporate the total annual wastewater volume plus the precipitation that would
fall on the pond. The system should be designed for the maximum wet year
and minimum evaporation year of record if overflow is not permissible under
any circumstances. Less stringent design standards may be appropriate in
situations where occasional overflow is acceptable or an alternative disposal
area is available under emergency conditions.
Monthly evaporation and precipitation rates must be known to properly
size the system. Complete retention ponds usually require large land areas, and
these areas are not productive once they have been committed to this type of
system. Land for this system must be naturally flat or be shaped to provide
ponds that are uniform in depth, and have large surface areas. The design
procedure for a complete retention wastewater pond system is available
elsewhere (USEPA, 1983).
COMBINED SYSTEMS
In certain situations it is desirable to design pond systems in combinations,
i.e., an aerated pond followed by a facultative or a tertiary pond. Combinations
of this type are designed essentially the same as the individual ponds. For
example, the aerated pond would be designed as described above, and the
predicted effluent quality from this unit would be the influent quality for the
facultative polishing pond. Further details on combined pond systems can be
found elsewhere (Boulier and Atchinson, 1980; Gloyna, 1976; and Rich, 1982).
Oswald (1970) has developed the Advanced Integrated Pond system (AIP)
which consists of four basic types of ponds in series (USDOE, 1993). A
facultative pond with a "digester pit" is followed by a high-rate pond, a settling
pond, and a maturation pond(s). Systems have been built in several locations
in California and several countries throughout the world. The best know facility
of this type is located in St. Helena, California.
r
ANAEROBIC PONDS
There is no agreement on the best approach to the design of anaerobic
stabilization ponds. Systems are designed on the basis of surface loading rate,
volumetric loading rate and hydraulic detention time. Although done frequently,
design on the basis of surface loading rate probably is inaccurate. Proper
design should be based on the volumetric loading rate, temperature of the
liquid, and the hydraulic detention time.
2-28
-------
Chapter 2
In climates where the temperature exceeds 22°C, the following design
criteria should yield a BOD5 removal of 50 % or better (WHO, 1987).
• Volumetric loading up to 300 g BOD5/m3-day
• Hydraulic detention time of approximately 5 days
• Depth between 2.5 and 5 meters
In cold climates, detention times as great as 50 days and volumetric
loading rate as low as 40 g BOD5/m3-day may be required to achieve 50%
reduction in BOD5 The relationship between temperature, detention time, and
BOD reduction is shown in Tables 2-4 and 2-5.
Table 2-4
Five-day BOD Reduction as a Function of Detention Time
for Temperatures Greater Than Twenty Degrees Celcius (WHO, 1987)
Detention Time BOD5 Reduction
(days) (%)
- _
2.5 60
5 70
Table 2-5
Five-day BOD Reduction as a Function of Detention Time, and
Temperature (WHO, 1987)
Temperature Detention Time BOD Reduction
(°C) (days) (%)
To 5 0-10
10-15 4-5 30-40
15-20 2-3 40-50
20-25 1-2 40-60
25-30 1-2 60-80
2-29
-------
Chapter 2
PATHOGEN REMOVAL
Bacteria, parasite, and virus removal is very effective in multiple-cell
wastewater stabilization ponds with suitable detention times (Reed, 1985). A
minimum of three cells is recommended. It is expected that the normal
detention time provided for BOD removal in most pond systems may be
sufficient to satisfy most regulatory requirements for bacteria and virus removal
without additional disinfection; however, a 20-day minimum detention time is
suggested.
SUSPENDED SOLIDS REMOVAL
j!
The occasional high concentration of SS, which can exceed 100 mg/l, in
the effluent is the major disadvantage of pond systems. The solids are
primarily composed of algae and other pond detritus, not wastewater solids.
These high concentrations are usually limited to 2 to 4 months during the year.
Several options, discussed in the sections to follow, are available for improving
system performance. Further details can be found in Middlebrooks et al.
(1982); USEPA (1973); USEPA (1974); USEPA (1981); USEPA (1974).
Intermittent sand filtration
Intermittent sand filtration is capable of polishing pond effluents at
relatively low cost. It is similar to the practice of slow sand filtration in potable
water treatment or the slow sand filtration of raw sewage which was practiced
during the early 1900s. Intermittent sand filtration of pond effluents is the
application of pond effluent on a periodic or intermittent basis to a sand filter
bed. As the wastewater passes through the bed, suspended solids and other
organic matter are removed through a combination of physical straining and
biological degradation processes. The particulate matter collects in the top 5 to
8 cm (2 to 3 in) of the filter bed, and this accumulation eventually clogs the
surface and prevents effective infiltration of additional effluent. When this
happens, the bed is taken out of service, the top layer of clogged sand
removed, and the unit is put back into service. The removed sand can be
washed and reused or discarded.
The effluent quality is almost totally a function of the sand gradation used.
When BOD and SS below 30 mg/l will satisfy requirements, a single-stage filter
with medium sand will produce a reasonable filter run. If better effluent quality
is necessary, a two-stage filtration system should be used, with finer sand in
the second stage.
2-30
-------
Chapter 2
Typical hydraulic loading rates on a single stage filter range from 0.37 to
0.56 m3/m2-day (0.4 to 0.6 million gallons/ac-day). If the SS in the influent to
the filter will routinely exceed 50 mg/l, the hydraulic loading rate should be
reduced to 0.19 to 0.37 m3/m2-day (0.2 to 0.4 million gallons/ac-day) to
increase the filter run. In cold weather locations, the lower end of the range
is recommended during winter operations to avoid the possible need for bed
cleaning during the winter months. The total filter area required for a single-
stage operation is obtained by dividing the anticipated influent flow rate by the
hydraulic loading rate selected for the system. One spare filter unit should be
included to permit continuous operation since the cleaning operation may
require several days. An alternate approach is to provide temporary storage in
the pond units. Three filter beds are the preferred arrangement to permit
maximum flexibility. In small systems that depend on manual cleaning, the
individualbed should not be bigger than about 90 m2 (1000 ft2). Larger
systems with mechanical cleaning equipment might have individual filter beds
up to 5000 m2 (55,000 ft2) in area.
Selected sand is usually used as the filter media. These are generally
described by their effective size (e.s.) and uniformity coefficient (u). The e.s.
is the 10 percentile size, i.e., only 10 percent of the filter sand, by weight, is
smaller than that size. The uniformity coefficient is the ratio of the 60
percentile size to the 10 percentile size. The sand for single-stage filters should
have an e.s. ranging from 0.20 to 0.30 mm and a u of less than 7.0, with less
than 1 percent of the sand smaller than 0.1 mm. The u value has little effect
on performance, and values ranging from 1.5 to 7.0 are acceptable. In the
general case clean, pit-run concrete sand is suitable for use in intermittent sand
filters providing the e.s., u, and minimum sand size are suitable.
The design depth of sand in the bed should be at least 45 cm (18 in) plus
a sufficient depth for at least 1 year of cleaning cycles. A single cleaning
operation may remove 2.5 to 5 cm (1 to 2 in) of sand. A 30-day filter run
would then require an additional 30 cm (12 in) of sand. In the typical case an
initial bed depth, of about 90 cm (36 in) of sand is usually provided. A graded
gravel layer 30 to 45 cm (12 to 18 in) separates the sand layer from the
underdrains. The bottom layer is graded so that its e.s. is four times as great
as the openings in the underdrain piping. The successive layers of gravel are
progressively finer to prevent intrusion of sand. An alternative is to use gravel
around the underdrain piping and then a permeable geotextile membrane to
separate the sand from the gravel. Further details on design and performance
of these systems can be found in Middlebrooks et al. (1982), Russell (1980),
and USEPA (1983).
2-31
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Chapter 2
Microstrainers
Early experiments with microstrainers to remove algae from pond effluents
were largely unsuccessful. This was generally attributed to the algae being
smaller than the mesh size of the microstrainers tested. A polyester fabric with
a 1-//m mesh size has since been developed, and it appears that microstrainers
equipped with this fabric are capable of producing an effluent with BOD and SS
concentrations less than 30 mg/l.
Microscreen manufacturers are promoting the use of the 1 -//m screen with
the return of the filtered algae to the pond. Short-term experience indicates
that the return of filtered algae does not cause problems; however, the
potential exists for the filtered material to accumulate and eventually cause
overloading of the screen. The effects of solids recycle through the pond
system should be monitored in newly constructed microscreen systems. The
first full-scale microstrainer application to pond effluent, a 7,200 m3/day (1.9
million gallon/day) unit was placed in operation in Camden, South Carolina in
December 1981 (Harrelson and Cravens, 1982). Typical design criteria include
surface loading rates of 90 to 120 m3/m2-day (1.5 to 2.0 gpm/ft2} and head
losses up to 60 cm (2 ft). Other process variables include drum speed,
backwash rate and pressure; these are normally determined on the basis of
influent quality and effluent expectations. The service life of the screen is
reported to be about 1 1/2 years, which is considerably less than the
manufacturer's prediction of 5 years. Difficulty with screen binding and short
run times was experienced with the Camden system. Before designing a
microscreen for pond polishing, careful study is recommended.
Rock filters
A rock filter operates by allowing pond effluent to travel through a
submerged porous rock bed, causing algae to settle out on the rock surfaces
as the liquid flows through the void spaces. The accumulated algae are then
biologically degraded. Algae removal with rock filters has been studied
extensively at Eudora, Kansas; California, Missouri; and Veneta, Oregon
(Swanson and Williamson, 1980; and USEPA, 1983). Many rock filters have
been installed throughout the United States and the world, and performance
has varied (Middlebrooks, 1988).
The principal advantages of the rock filter are its relatively low
construction cost and simple operation. Odor problems can occur, and the
design life for the filters and the cleaning procedures have not yet been firmly
established. However, several units have operated successfully for 10 to 15
years.
2-32
-------
Chapter 2
Other solids removal techniques
A detailed discussion of normal granular media filtration, dissolved air
flotation, autoflocculation, phase isolation, centrifugation, and coagulation-
flocculation is presented in Middlebrooks et al. (1982) and USEPA (1983).
These techniques are used infrequently, but the designer should be aware of
their potential.
NITROGEN REMOVAL
The BOD and SS removal capability of pond systems has been reasonably
well-documented, and reliable designs are possible; however, the nitrogen
removal capability of wastewater ponds is given little consideration in most
system designs. Nitrogen removal can be critical in many situations, since
ammonia nitrogen in low concentrations can adversely affect some young fish
in receiving waters. In addition, nitrogen is often the controlling parameter for
design of land treatment systems. Any nitrogen removal in the preliminary
pond units can result in a very significant savings in the land area required and
therefore the costs for land treatment (Reed et al., 1995).
Nitrogen loss from streams, lakes, impoundments, and wastewater ponds
has been observed for many years. Data on nitrogen losses have been
insufficient for a comprehensive analysis, and there has been no agreement on
the removal mechanisms. Various investigators have suggested: algal uptake,
sludge deposition, adsorption by bottom soils, nitrification/denitrification and
loss of ammonia as a gas to the atmosphere (volatilization). Several
evaluations suggest that a combination of factors may be responsible, with the
dominant mechanism under favorable conditions being losses to the atmosphere
(Pano and Middlebrooks, 1982; Reed, 1984; USEPA, 1983).
The EPA sponsored comprehensive studies of wastewater pond systems
in the late 1970s. These results provided absolute verification that significant
nitrogen removal does occur in pond systems. Table 2-6 summarizes the key
findings from these studies, which confirm that nitrogen removal is in some
way related to pH, detention time, and temperature in the pond system. The
pH fluctuates as a result of the algae-carbonate interactions in the pond, so
wastewater alkalinity is important. Under ideal conditions, up to 95 percent
nitrogen removal can be achieved in wastewater stabilization ponds.
2-33
-------
Chapter 2
Table 2-6
Data Summary From EPA Pond Studies (USEPA, 1983)
Location
Peterborough, NH
3 cells
Kilmichael, MS
3 cells
Eudora, KS
3 cells
Corinne, UT
1st 3 cells
Detention
Time
(days)
107
214
231
42
Water
Temperature
rc)
11
18.4
14.7
10
PH
(median)
7.1
8.2
8.4
9.4
Alkalinity
(mg/l)
85
116
284
555
Influent
Nitrogen
(mg/l)
17.8
35.9
50.8
14.0
Removal
(%)
43
80
823
46
Design models
Data were collected on a frequent schedule from every cell at all of the
pond systems listed in Table 2-6 for at least a full annual cycle. This large
body of data allowed quantitative analysis with all major variables included, and
two design models were independently developed. These have been validated
using the same data from sources not used in the model development. The
two models are summarized in Tables 2-7 and 2-8; details on development of
Model 1 can be found in Reed (1984) and details of Model 2 can be found in
Pano and Middlebrooks (1982).
Design Model Number 1 (Reed, 1984)
A/e=A/0 exp {-kt [f+60.6(p/y-6.6)] (17)
where Ne = effluent total nitrogen, mg/l
N0 = influent total nitrogen, mg/l
kT = temperature dependent, rate ponstant, days"1, pH"1
= k20(0)T-20 ;
e = 1.039
T = water temperature, (use Eq. 13)
2-34
-------
Chapter 2
k20 = 0.0064 day'1
See Reed (1984) or USEPA (1983) for typical pH values or estimate with:
pH = 7.3 exp[0.0005(ALK)]
ALK = expected influent alkalinity, mg/l, (derived from data in Reed,
1984 and USEPA, 1983)
Table 2-8
Design Model Number 2 {Pano and Middlebrooks, 1982 and USEPA, 1983)
A/=A/
e~/vO
1 +f(0.0005767-0.00028)exp[(1.080-0.0427) (pH-Q. 6)]
(18)
All terms defined in Table 2-7.
Both are first order models, and both depend on pH, temperature, and
detention time in the system. Although they both predict the removal of total
nitrogen, it is implied in the development of each that volatilization of ammonia
is the major pathway for nitrogen removal from wastewater stabilization ponds.
Figure 2-4 demonstrates the application of the two models and compares the
predicted total nitrogen in the effluent to the actual monthly average values
measured at Peterborough, New Hampshire.
Both of these models are written in terms of total nitrogen, and they
should not be confused with the still valid equations in Pano and Middlebrooks
(1982) and USEPA (1983), which are limited to only the ammonia fraction.
Calculations and predictions based on total nitrogen should be even more
conservative than those earlier models.
The high-rate ammonia removal by air stripping in advanced wastewater
treatment depends on high (> 10) chemically adjusted pH. The algal-carbonate
interactions in wastewater ponds can elevate the pH to similar levels for brief
periods. At other times, at moderate pH levels the rate of nitrogen removal
may be low, but the long detention time in the pond compensates.
2-35
-------
Chapter 2
Model 1
A Mode! 2
Ice'cbvered-
II ! Ill I II
J F . M A M J
A S 0 N D
FIGURE 2-4 PREDICTED VERSUS ACTUAL EFFLUENT NITROGEN, PETERBOROUGH, N.H.
2-36
-------
Chapter 2
Application
These models should be useful for new or existing wastewater ponds
when nitrogen removal and/or ammonia conversion is required. The design of
new systems would typically base detention time on the BOD removal
requirements. The nitrogen removal that will occur during that time can then
be calculated with either model. It is prudent to assume that the remaining
nitrogen in the effluent will be ammonia, and to then design any further removal
/conversion for that amount. If additional land area is available, a final step can
be a comparison of the costs of providing additional detention time in the pond
for nitrogen removal with the costs for other removal alternatives.
PHOSPHORUS REMOVAL
The need for phosphorus removal can occur when eutrophication is an
issue. In general, phosphorus removal is not often required for wastewaters
receiving stabilization pond treatment, but there are a number of exceptions for
systems in the north central United States and Canada (Reed et al., 1995).
Batch chemical treatment
In order to meet a phosphorus requirement of 1 mg/I for discharge to the
Great Lakes an approach using in-pond chemical treatment in controlled
discharge ponds was developed in Canada. Alum, ferric chloride and lime were
all tested by using a motor boat for distribution and mixing of the chemical. A
typical alum dosage might be 150 mg/I, and this should produce an effluent
from the controlled discharge pond that contains less than 1 mg/I of
phosphorus and less than 20 mg/I BOD and SS. The sludge build-up from the
additional chemicals is insignificant and would allow years of operation before
requiring cleaning. The costs for this method were very reasonable and much
less than conventional phosphorus removal methods (Graham and Hunsinger,
undated).
Continuous overflow chemical treatment
Studies of in-pond precipitation of phosphorus, BOD, and SS were
conducted over a 2 year period in Ontario, Canada (Graham and Hunsinger,
1977). The primary objective of the chemical dosing process was to test
removal of phosphorus with ferric chloride, alum and lime. Ferric chloride doses
of 20 mg/I and alum doses of 225 mg/I, when continuously added to the pond
influent, effectively maintained pond effluent phosphorus levels below 1 mg/I
over a 2-year period. Hydrated lime, at dosages up to 400 mg/I, was not
effective in consistently reducing phosphorus below 1 mg/I ( 1 to 3 mg/I was
2-37
-------
Chapter 2
achieved) and produced no BOD reduction while slightly increasing the SS
concentration. Ferric chloride reduced effluent BOD from 17 to 11 mg/l and SS
from 28 to 21 mg/l; alum produced no BOD reduction and a slight SS reduction
(from 43 to 28-34 mg/l). Consequently, direct chemical addition appears to be
effective only for phosphorus removal.
A six cell pond system located in Waldorf, Maryland, was modified to
operate as two three-cell units in parallel (Engel and Schwing, 1980). One
system was used as a control and alum added to the other for phosphorus
removal. Each system contained an aerated first cell. Alum addition tp the
third cell of the system proved to be more efficient in removing total
phosphorus, BOD, and SS than alum addition to the first cell. Total phosphorus
reduction averaged 81 percent when alum was added to the inlet to the third
cell and 60 percent when alum was added to the inlet of the first cell. Total
phosphorus removal in the control ponds averaged 37 percent. When alum
was added to the third cell, the effluent total phosphorus concentration
averaged 2.5 mg/l, with the control units averaging 8.3 mg/l. Improvements
in BOD and SS removal by alum addition were more difficult to detect, and at
times increases in effluent concentrations were observed.
PHYSICAL DESIGN AND CONSTRUCTION
Regardless of the care taken to evaluate coefficients and apply biological
or kinetic models, if sufficient consideration is not given to optimization of the
pond layout and construction, the actual efficiency may be far less than the
calculated efficiency. The physical design of a wastewater pond is as
important as the biological and kinetic design. The biological factors affecting
wastewater pond performance are primarily employed to estimate the required
hydraulic residence time to achieve a specified efficiency. Physical factors,
such as length to width ratio, will determine the actual efficiency achieved
(Middlebrooks et al.; 1982; USEPA, 1983).
Length to width ratios are determined according to the design model used.
Complete-mix ponds should have a length to width ratio of approximately 1:1;
whereas, plug-flow ponds require a ratio of 3:1 or greater.
The danger of groundwater contamination may impose seepage
restrictions, necessitating lining or sealing the pond. Reuse of pond effluents
in dry areas where all water losses are to be avoided may also dictate the use
of linings. Layout and construction criteria should be established to reduce dike
erosion from wave action, weather, rodent attacks, etc. Transfer structure
2-38
-------
Chapter 2
placement and size affect flow patterns within the pond and determine
operational capabilities in controlling the water level and discharge rate.
Dike construction
Dike stability is most often affected by erosion caused by wind driven
wave action or rain and rain-induced weathering. Dikes may also be destroyed
by burrowing rodents. A good design will anticipate these problems and
provide a system which can, through cost-effective operation and maintenance,
keep all three under control.
Erosion protection is necessary on all slopes; however, if winds are
predominantly from one direction, protection should be emphasized for those
areas that receive the full force of the wind driven waves. Protection should
extend from at least 0.3 m (1 ft) below the minimum water level to at least 0.3
m (1 ft) above the maximum water surface. Asphalt, concrete, fabric, low
grasses, and riprap have all been used to provide protection form wave action.
The use of rip rap, however, can make weed and rodent control more difficult.
In some cases when fabric liners are used, a covering of rip rap is also used to
protect the plastic materials from damaging ultraviolet radiation from the sun.
Rodent control can be achieved with earthen dikes by periodically changing the
water levels to flood the burrows. The selection of proper soils and compaction
during construction can render an earthen dike essentially impermeable.
,Seepage collars should be provided around any pipe penetrating the dike; these
collars should extend a minimum of 0.6 m (2 ft) from the pipe.
Pond sealing
The primary motive for sealing ponds is to prevent seepage, which can
pollute groundwaters and affect treatment performance by causing fluctuations
in the water depth. Sealing methods can be grouped in three categories:
• Synthetic and rubber liners
• Compacted earth or soil cement liners
• Natural and chemical treatment liners
Within each category also exists a wide variety of application
characteristics. Choosing the appropriate lining for a specific site is a critical
factor in pond design and seepage control. Seepage rates range from 0.003
cm/day (0.001 in/day) for synthetic membranes to about 10 cm/day (4 in/day)
for soil cement liners (USEPA, 1983). Detailed information is available from
2-39
-------
Chapter 2
manufacturers and in other publications (Kays, 1986; and Middlebrooks, et al.,
1978).
Pond hydraulics
In the past, the majority of ponds were designed to receive influent
wastewater through a single pipe, usually located toward the center of the first
cell in the system. Hydraulic and performance studies 7'9-19-20 have shown that
the center discharge point is not the most efficient method of introducing
wastewater to a pond (Finney and Middlebrooks, 1980; George, 1973;
Mangelson, 1971, 1972). Multiple inlet arrangements are preferred even in
small ponds [<0.5 ha (<1.2 ac)]. The inlet points should be as far apart as
possible and the water should preferably be introduced by means of a long
diffuser or multiple inlet structure. The inlets and outlets should be placed so
that flow through the pond is uniform between successive inlets and outlets.
Single inlets can be used successfully if the inlet is located the greatest
distance possible from the outlet structure and is baffled, or the flow is
otherwise directed to avoid currents and short circuiting. Outlet structures
should be designed for multiple-depth withdrawal, and all withdrawals should
be a minimum of 0.3 m (1 ft) below the water surface to reduce the potential
impact of algae and other surface detritus on effluent quality.
Analysis of performance data from selected aerated and facultative ponds
indicates that four cells in series are desirable to give the best BOD and fecal
coliform removals for ponds designed as plug-flow systems. Good performance
can also be obtained with a smaller number of cells if baffles or dikes are used
to optimize the hydraulic characteristics of the system.
Better treatment is obtained when the flow is guided more carefully
through the pond. In addition to treatment efficiency, economics and
aesthetics play an important role in deciding whether or not baffling is
desirable. In general, the more baffling that is used, the better the flow control
and treatment efficiency. The lateral spacing and length of the baffle should
be specified so that the cross-sectional area of flow is as close to a constant
as possible.
Wind generates a circulatory flow in bodies of water. To minimize short
circuiting due to wind, the pond inlet-outlet axis should be aligned perpendicular
to the prevailing wind direction if possible. If this is not possible, baffling can
be used to control to some extent the wind-induced circulation. In a constant-
depth pond the surface current will be in the direction of the wind, and the
return flow will be in the upwind direction along the bottom.
2-40
-------
Chapter 2
Ponds that are stratified because of temperature differences between the
inflow and the pond contents tend to behave differently in winter and summer.
In summer the inflow is generally colder than the pond, so it sinks to the pond
bottom and flows toward the outlet. In the winter the reverse is generally true,
and the inflow rises to the surface and flows toward the outlet. A likely
consequence is that the effective treatment volume of the pond is reduced to
that of the stratified inflow layer (density current). The result can be a drastic
decrease in detention time and an unacceptable level of treatment.
STORAGE PONDS FOR LAND TREATMENT SYSTEMS
Seasonal effluent storage ponds are sometimes required for land treatment
systems. Storage is necessary for all nonoperationai periods at the land
treatment system and is desirable for flow equalization and emergency system
back-up. Nonoperating periods may be due to climate, planting or harvesting
and other maintenance operations. The design storage volume is determined
from a calculated water balance during design (Reed et al., 1995).
The storage pond may follow other conventional treatment units or may
be the final cell in a stabilization pond system. The storage cell is usually
deeper than typical treatment pond cells and can range from 3 to 6 m (9 to 1 8
ft) in depth. Credit should be taken during design for the additional treatment
which will occur in this storage pond, using the methods presented herein.
Calculation of nitrogen removal using either Eq. 17 or 18 is particularly
important. Nitrogen is often the limiting design factor for land treatment
systems, directly affecting the land area required for treatment. Any nitrogen
removal in the storage pond will reduce the final treatment area and the costs.
Similarly, the pathogen removal in the pond can often satisfy requirements
without further disinfection.
The operation of the storage pond will depend on the type of land
treatment system in use. Storage is usually only provided for emergencies in
rapid infiltration systems so the pond is drained as soon as it is possible to do
so. Since overland flow systems are not very effective for algae removal,
storage ponds for these systems are bypassed during algal bloom periods, and
the ponds drawn down when algae concentrations are low. Algae are not a
concern for slow rate land treatment, so the storage pond may stay on line
continuously. This is necessary if nitrogen or pathogen removal is expected in
the storage cell. In this case, treated wastewater flow into the cell should
continue on a year-round basis, and the withdrawals should be scheduled for
attainment of the specified water depth at the end of the operating season for
the land treatment component.
2-41
-------
-------
CHAPTER 3
MEXICALI, BAJA CALIFORNIA NORTE (BCN)
MEXICO WASTEWATER TREATMENT SYSTEM
-------
-------
Chapter 3
CHAPTER 3
MEXICALI, BAJA CALIFORNIA NORTH (BCN),
MEXICO WASTEWATER TREATMENT SYSTEM
Mexicali, Mexico is located in the Northwest part of the state of Baja,
California, and the New River flows through the city. Effluent from the two
wastewater stabilization pond systems in Mexicali discharge into the New River
as well as the effluent from industrial operations and agricultural drains.
The sewer system is divided into two sections, Mexicali I, the older more
established section of the city, and Mexicali II which is still developing in
conjunction with industrial operations. The current population of the city is
539,000 inhabitants, and the population is expected to grow to 941,000 by
the year 2015. Wastewater flow rates are expected to be 1,645 liters per
second (37.6 MGD) in 2015. Parts of Mexicali II currently are not sewered, and
when the current flow rate into the Mexicali I pond system is considered, the
2015 design flow rate is currently being approached and likely will increase
beyond the projections.
Wastewater from Mexicali II is partially treated in the Gonzalez Ortega
pond system which is heavily overloaded. The Mexicali BCN Lagoon System
I (MLSI) receives wastewater from the Zaragoza neighborhood, and the system
is less stressed but still overloaded.
SYSTEM DESCRIPTION
A plan view of the Mexicali BCN I lagoon system is shown in Figure 2-1,
and a simplified flow diagram of the system is shown in Figure 2-2. The
system consists of three anaerobic ponds (designed as aerated ponds) followed
by two trains of facultative ponds. Train A consists of six facultative ponds
receiving one-half of the combined flow from the three primary (anaerobic)
ponds, and train B has four facultative ponds receiving the remaining half of the
flow from the three anaerobic ponds. All three primary ponds have equal
volumes, and surface areas. Although shaped differently, all ten of the
facultative ponds have the same volume and surface area. The sizes of the
primary and facultative ponds are presented in Figure 2-2. The volume of the
cells, hydraulic detention time in each cell, and the total detention time for the
system are shown in Table 2-1. These data were used to develop the
relationships presented in the following sections.
3-1
-------
Chapter 3
FIGURE 3-1 PLAN VIEW OF MEX.CALI, MEXICO WASTEWATER STABILIZATION
POND SYSTEM (MEXICALI I) ABILIZA1 ION
3-2
-------
Raw
Wastewater
Chapter 3
T
Primary # 1
Primary # 2
Secondary #1
Secondary #2
Secondary #3
Secondary #4
Secondary #5
Secondary #6
Primary #3
Secondary #1A
Secondary #2A
Secondary #3A
Secondary #4A
11
TYPE NO. CELLS AREA
ACRES
DEPTH TOTAL AREA
FEET ACRES
PRIMARY 3
SECONDARY 10
21.67
36.45
15.1
4.3
65.0
364.5
1
To New River
Pumping Wet
Well Discharging
to Irrigation System
FIGURE 3-2
SCHEMATIC OF MEXICALI BCN, MEXICO WASTEWATER
STABILIZATION LAGOON SYSTEM
3-3
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3-4
-------
Chapter 3
PERFORMANCE OF SYSTEM
Design Limitations
The MLSI was designed as an aerated pond system, but power was not
supplied to the aerators; therefore, the system operates as an anaerobic pond
system followed by facultative ponds. Had the ponds been operated as
designed, the system would produce an excellent quality effluent in terms of
BOD removal. Proper design, location and control of a settling basin would
have resulted in a far superior quality effluent overall.
Performance of Anaerobic Ponds
The performance of anaerobic ponds has not been documented as well
as it has for aerated or facultative ponds; however, there are enough data
available to make a reasonable estimate of the expected performance at various
water temperatures. The variation in BOD removal with temperature shown in
Figure 3-3 was taken from a World Health Organization document (1 987), and
the line of best fit was determined to be the following exponential curve.
or
% BOD /?e/77ovc?/=60.61(ln Tempera tore)- 130. 06
Using the above equations and the observed water temperatures in the
Mexicali BCN I pond system, the performance of the anaerobic ponds was
estimated and the results are shown in Table 3-2.
Effluent Characteristics
A summary of the performance data and the effluent characteristics for
the Mexicali BCN I lagoon system is shown in Table 3-3. Until January 1994
the pond system appeared to be consistently producing an effluent BOD of less
than 30 mg/l. Since then the BOD effluent quality has varied considerably, and
the BOD concentration has frequently approached or exceeded 40 mg/l. The
variations in BOD, COD, and water temperature are shown in Figure 3-4 . Fecal
coliform numbers also have tended to increase during this period while the
dissolved oxygen in the effluent has declined (Figure 3-5 and Figure 3-6).
These changes are probably attributable to the increase in influent flow rate
caused by population growth and additional sewer connections.
3-5
-------
Chapter 3
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Chapter 3
The variations in flow rate, dissolved oxygen and Ph value are shown in
Figure 3-6. The Ph value varied very little over the 30 months, but dissolved
oxygen tended to decrease as the pond system matured. This drop in dissolved
oxygen was caused by the increasing load being applied to the system.
BOD Loadings and Loading Rates
BOD loadings and loading rates for the primary cells and Train A and B
are shown in Table 3-2. BOD loading rates on all components of the system
are high and the system is performing as well as can be expected. The loading
rate on each of the six facultative ponds is approximately two-thirds of that
applied to the four facultative ponds; however, observers of the system report
that at most times the effluent from Train B is clearer than that coming! from
Train A. Based upon the characteristic of the two trains, there does not appear
to be any reason to expect the quality to differ unless the detention time in
Train B ponds is such that the algae production is less. This does not appear
to be the case, because both detention times are adequate to produce
considerable algae concentrations.
BOD vs Hydraulic Detention Time
Variations in the effluent BOD concentration, system hydraulic detention
time, and the water temperature for the 30 months that performance data were
available are shown in Figure 3-7. In general, the effluent BOD improved with
an increase in water temperature; however, there was no significant change in
BOD with changes in hydraulic detention time.
The relationship between effluent BOD and the system hydraulic
detention time is shown in Figure 3-8. There is a downward trend in the
effluent BOD as the hydraulic detention time increases; however/ the
coefficient of determination (R2) is only 0.103 which is not statistically
significant. This result is not surprising because the influent flow rate is only
a rough estimate of the actual flow rate.BOD versus BOD Loading Rate
The variations in the effluent BOD concentration with the BOD loading
rate on the secondary (facultative) ponds, Train A and B, are shown in Figures
3-9 and 3-10. The relationships show an increase in the effluent BOD
concentration as the BOD loading rate increases, and the relationships are
statistically significant at the 95 % confidence level.
3-12
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Chapter 3
BOD-Temperature
When influent and effluent BOD values and water temperature are
available, it is possible to develop an equation showing a rate relationship
between the BOD and temperature. Unfortunately, influent BOD values were
unavailable, but if it is assumed that the influent BOD is relatively constant and
that the effluent BOD is related to the water temperature, predictive
relationships can be developed that are similar to those developed from the
Arrhenius equation. A relationship can be developed from either a simple plot
of the natural logarithm of the effluent BOD versus water temperature (Figure
3-11) or a quasi-Arrhenius plot of effluent BOD divided by the BOD at 20
degrees celsius versus the water temperature minus 20 degrees Celsius (Figure
3-12). Both relationships yield a statistically significant (R2 = 0.460, 95%
confidence level) relationship and yield the same answer when using either
equation because the numbers are divided by a constant to yield the quasi-
Arrhenius plot.
Although these relationships lack precision, the results are as good or
superior to those developed from numerous other sets of pond performance
data. There are too many variables affecting the performance of pond systems
for one to expect the relationship between effluent BOD and temperature to be
perfectly correlated (Middlebrooks et al., 1982, USEPA, 1983).
Temperature Corrected BOD and Detention Time
Using the relationships developed between effluent BOD and water
temperature, a corrected effluent BOD was calculated and plotted versus the
hydraulic detention time (Figure 3-13). As shown in Figure 3-13, the
relationship between the two variables was poorer than that observed in Figure
3-8 when the effluent BOD was uncorrected. Again, this is not surprising
because similar results have been observed when analyzing pond performance
data (Middlebrooks et al., 1982, USEPA, 1983).
PREDICTED PERFORMANCE
In an effort to predict the performance of the Mexicali BCN I pond
system, a linear correlation was conducted with the effluent BOD as the
independent variable and the BOD loading rate on the facultative ponds, the
water temperature, and the BOD loading rate on the anaerobic ponds as the
dependent variables. The following relationship was obtained when the outlier
value of 71 mg/l was excluded.
Eff.BOD=1.732(BOD Load.Rate on Sec.)+3.149(7e/77p.)-0.054(£OD Load. Rate on Pri.)
3-17
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3-20
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Chapter 3
A plot of the predicted values versus the measured values is shown in
Figure 3-14. Although less precise than desired, the points lie around the 45
degree line, and the equation would be expected to yield a reasonable estimate
of the performance of the Mexicali BCN I system in view of the limitations of
the flow measurements.
REDESIGN OF MEXICALI BAJA CALIFORNIA NORTE (BCN) I SYSTEM
Calculations were made using Equations 10 and 1 1 taken from the body
of the report to determine the performance of the Mexicali BCN I pond system
when converting the primary and secondary ponds to complete mix or partial
mix or a combination of the two types.
where Cn = effluent BOD concentration in cell n, mg/l
C0 = influent BOD concentration, mg/l
kp and kc = first order reaction rate constant, days"1
kp= 0.276 day'1 at 20° C (assumed to be constant in all cells)
kc = 2.0 day'1 at 20° C (assumed to be constant in all cells.)
t = total hydraulic residence time in pond system, days
n = number of cells in the series.
If other than a series of equal volume ponds are to be employed, it is
necessary to use the following general equation:
/If / 1
— I I I w w I I
f1j [l+k2^ [/+*ntn* (11)
3-21
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Chapter 3
The predicted performances based on the design temperature of 12° C, an
influent BOD of 300 mg/l, and the current estimated flow rates for several
combinations of complete mix and partial mix pond systems are presented in
Table 234. Converting the primary cells (anaerobic) to complete mix ponds
would produce an effluent BOD of less than 25 mg/l throughout the 30 months
of record. When converting the primary cells to partial mix ponds, an effluent
BOD ranging from 59 to 84 mg/l would be produced. Converting the ponds to
two partial mix cells of equal volume in series would yield an effluent BOD
concentration of 11 to 23 mg/l. The remaining volume would provide an
excess of settling time, and it would be necessary to account for this excess
volume. The effluent BOD would range between 7 and 20 mg/l when operating
the primary cells and the two (Trains A and B) secondary trains as partial mix
pond systems. Converting the primary cells to complete mix and the Train A
'(six cells) cells to partial mix would result in an effluent BOD concentration of
two to five mg/l.
Table 3-5 contains the results for the same combinations presented in
Table 3-4, but the flow rate has been increased to twice that of the current
flow rates. If the objective is to produce an effluent with a BOD concentration
of 30 mg/l or less at twice the current flow rate, the only combination that will
yield the desired quality is to convert the primary cells to complete mix and the
secondary cells to partial mix pond systems.
Increasing the flow rate to 1.5 times the current flow rates for the same
conditions described for Table 3-4 and 3-5, the system would be able to
produce an effluent satisfying a 30 mg/l BOD standard with the conversion of
the primary and secondary cells to partial mix pond systems and the use of a
complete mix pond in the primary followed by partial mix cells in the secondary
ponds (Table 3-6).
To control the solids concentrations in the effluent, it will be necessary to
redesign the effluent structures to provide multiple draw-off structures with
multiple draw-off depths. It may be necessary to improve the hydraulics of the
system with floating baffles or dikes. It was impossible to determine if the flow
was evenly distributed to the three primary cells; therefore, it probably will be
necessary to construct new inlet structures as well.
Based upon the standard design equations shown above, it is possible to
make relatively simple conversions to the Mexicali BCN I pond system that
would result in a good quality effluent at a relatively small cost.
3-23
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Chapter 3
Tables 3-7 through 3-9 were developed for the same flow patterns used
in Tables 3-4 through 3-6, but the predictions are based on the measured water
temperature and the current flow rates, two times the current flow rate, and
1.5 times the current flow rate. Because the design temperature was the
lowest temperature reported for the 30 months of sampling, the results from
the various combinations of partial and complete mix ponds for the observed
operating temperatures were equal to or superior to those reported in Tables 3-
4 through 3-6.
3-27
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3-30
-------
CHAPTER 4
NOGALES INTERNATIONAL
WASTEWATER TREATMENT PLANT
-------
-------
Chapter 4
CHAPTER 4
NOGALES INTERNATIONAL WASTEWATER TREATMENT PLANT
The Nogales International Wastewater Treatment Plant (NIWTP) is
located on the USA side of the border, and receives approximately two-thirds
of the plant influent flow from the Mexican side of the border. The wastewater
from the Mexican side of the border is a combination of storm runoff and
domestic and industrial wastewater. The wastewater being treated by the
NIWTP is a relatively weak sewage because of the dilution from the stormwater
events and groundwater infiltration.
The Nogales plant was designed to treat an annual mean flow rate of
15.75 MGD and a peak flow of 28 MGD. The ultimate mean design flow is
17.2 MGD with the addition of aerators. The system currently is treating an
annual mean flow rate of 14.9 MGD. Flow from Nogales, Sonora is estimated
to increase to 32.3 MGD by the year 2020 with relatively small increases
projected for Nogales, Arizona.
SYSTEM DESCRIPTION
A plan view of the NIWTP is shown is Figure 4-1. The NIWTP has
extensive preliminary treatment consisting of screening and degritting.
Preliminary treatment is followed by two parallel trains of secondary treatment
with each train having a complete mix lagoon followed by four partial mix
lagoons. Only three of the partial mix lagoons are in service with the fourth
used to dry settled solids for removal. The lagoon system is followed by five
dual media automatic backwash filters for solids removal prior to disinfection
with an ultraviolet facility.
The preliminary treatment was added after the plant was constructed
because of very large concentrations of grit in the wastewater. Based on the
average daily flow rate of 15.75 MGD, the plant produces about 2 cubic yards
of grit each day, and the total volume of grit and screenings is approximately
4 cubic yards per day.
4-1
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Chapter 4
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Chapter 4
DESIGN ANALYSIS
Design Assumptions
When using any of the conventional formulas and removal rate constants
for the design of the Nogales plant, it is not possible to obtain the effluent BOD
concentration predicted in the operations manual. It appears that the designer
made an incorrect assumption that having two trains of equal volume would
double the detention time or it was assumed that a removal rate constant of
6.0 per day for the complete mix lagoon was acceptable. In either case, the
quality of the effluent was over estimated.
Based on conventional formulas and rate constants between 2.0 and 3.0
and using Equation 10, the effluent BOD concentration will range between 53
and 72 mg/l. Calculations are shown below for rate constants ranging from 2.6
to 6.0 per day.
,10)
where Cn = effluent BOD concentration in cell n, mg/l
C0 = influent BOD concentration, mg/l
k = first order reaction rate constant, days"1
= 2.0 day"1 at 20°C (assumed to be constant in all cells).
t = total hydraulic residence time in pond system, days
n = number of cells in the series.
When kc = 2.0 per day:
C-
260
When kc = 2.5 per day:
4-3
-------
Chapter 4
Ce= 26° 260
When kc = 3.0 per day:
260 260
+3.0(1.3))
When kc = 4.0 per day:
260
When kc = 5.0 per day:
~ 260 260
=35/77gr//
When kc = 6.0 per day:
260
(1+6.0(1.3))
Design Predictions
The NIWTP was designed for an annual mean flow rate of 1 5.75 MGD ancl
an ultimate mean flow of 17.2 MGD and an influent and effluent BOD of 260
and 30 mg/l, respectively. The following calculations were made to predict the
performance for various combinations of complete and partial mix aerated poncl
systems at 20 °C and 1 1 °C.
4-4
-------
Chapter 4
20 °C. At the design BOD concentration of 260 mg/l and a flow rate of
15.75 MGD, the following results were obtained.
C^=.
260
-=72mg//
72
-=24mg/f
The two complete mix cells are followed by two partial mix cells.
cep2=-
24
1+0.276 _
r = 1 5/770/7
With three complete mix cells in series (the original CM cell and the
conversion of two of the partial mix cells to CM) at the above conditions, the
following was obtained.
72
1+2I
-=8mg//
At 20 °C the design will produce an effluent that will satisfy the effluent
standard of 30 mg/l of BOD. Better solids control can be exercised by better
design of overflow structures and a reduced hydraulic residence time in the
settling basins.
4-5
-------
Chapter 4
11 °C. The following effluent BOD concentrations were calculated for a
design flow rate of 15.75 MGD and a design BOD concentration of 260 mg/l.
Cec1= „ °° _=. 260 ^ = 116 mflr//
n
mgll
The two complete mix cells are followed by two partial mix cells.
— =41 mgll
If three partial mix cells are converted to three complete mix cells in
series, the effluent quality will improve to 15 mg/l, and one "partial mix" cell
will remain for settling. If the remaining "partial mix" were converted to a true
partial mix cell rather than a settling cell, the effluent BOD concentration would
be 21 mg/l.
Similar calculations are shown for actual operating conditions and
increased flow rates in Tables 4-1 through 4-4. The physical characteristics of
the NIWTP lagoons are shown in Table 4-1 along with the influent and effluent
characteristics for the system. Table 4-2 shows the predicted performance for
various combinations of partial and complete mix cells at 11 degrees Celsius
and the measured temperature and flow rate. The predicted effluent from the
existing complete mix aerated lagoon shows that the system cannot meet the
predicted effluent quality as specified in the operations manual. By modifying
the system to various combinations of complete and partial mix aerated
lagoons, the system will be able to produce an excellent quality effluent in
terms of BOD.
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4-10
-------
Chapter 4
Using the same flow configurations as mentioned above but doubling the
flow rate, it can be seen from the results in Table 4-3 that with the proper
modifications the lagoon system is capable of producing an excellent effluent.
By tripling the design flow rate and with the correct combinations of complete
and partial mix cells, the system can be modified to produce an effluent BOD
concentration of 30 mg/l or less.
With relatively simple modifications in the existing lagoon system, it is
possible to significantly increase the flow rate to the system and produce an
acceptable effluent BOD concentration. Modifications of the settling ponds to
incorporate multiple drawoff structures and multiple drawoff levels and the
utilization of the proper hydraulic residence time should improve the TSS
effluent quality.
Oxygen Requirements
Complete Mix Cell. Determination of the oxygen requirements for the
complete mix pond system were verified using Equation 16 shown below.
where
(16)
N = equivalent oxygen transfer to tap water at standard conditions
kg/hr
Na = oxygen required to treat the wastewater, kg/hr (usually taken
as 1.5 x the organic loading entering the cell)
a= (oxygen transfer in wastewater)/(oxygen transfer in tap water)
= 0.9
CL = minimum DO concentration to be maintained in the
wastewater, assume 2 mg/l
Cs = oxygen saturation value of tap water at 20°C and one
atmosphere pressure = 9.17 mg/l.
Tw = wastewater temperature, °C. Assume 23 °C for checking.
4-11
-------
Chapter 4
Csw = P(CSS)P = oxygen saturation value of the waste, mg/l.
P = (wastewater saturation value)/tap water oxygen saturation
value) = 0.9
Css = tap water oxygen saturation value at temperature Tw, (see
Standard Methods or standard textbooks).
P = ratio of barometric pressure at the pond site to barometric
pressure at sea level, (assume 1.0 for an elevation of 100 m)
The design organic load in the influent wastewater is:
(C0)(Q) = (260g/m3)(65,102m3/day)(day/24hr)(kg/1000g) = 705 kg/h
The oxygen demand is assumed to be 1.5 times the organic loading, hence
NB1 = (1.5H705 kg/hr) = 1,058 kg/h
Use Eq. 16 to calculate equivalent oxygen transfer.
g{ Csw °L] 1.0257""-20
Csw = GSHCJIP) = (0.9){8.68 mg/l)(1.0) = 7.81 mg/l
1058
. = 1723 kg/h of oxygen
g
7. 81-2.0
A value of 1.9 kg O2/kWh (1.4kg/hp/h) is recommended for estimating
power requirements for surface aerators.
The total power for surface aeration in the complete mix cells:
(1723 kg/h of O2)/(1.9 kg/kWh of O2) = 907 kW (1,216 hp)
4-12
-------
Chapter 4
These surface aerator power requirements must be corrected for gearing and
blower efficiency. Assuming 90 percent efficiency for both gearing and
blowers, the total power for surface aerators in the complete mix cells would
be 907 kW/ 0.9 = 1,008 kW (1,351 hp) or 504 kW (676 hp) per complete mix
cell. Eleven 60 hp aerators were installed in each complete mix cell. This is
excellent agreement considering that only minor changes in assumptions could
result in differences greater than 16 hp.
Partial Mix Cells. An estimate of the oxygen transferred by the two 20
hp aerators in each "partial mix" cell can be made as follows.
Aerators transfer approximately 1.9 kg O2/kWh
Total of 40 hp x 0.7457 = 30 kW
Oxygen transfer = 30 kW x 1.9 kg O2/kWh = 57 kg Oxygen per hour
BOD loading to "PM" cells:
74 mg/l x (15.75 MGD/2) x 8.34 = 4,860 pounds per day = 2,209
kg/day = 92 kg/h x 1.5 = 151 kg/h
Therefore, the aerators in the "PM" cells are designed to provide
approximately 38 % of the design load applied to the first "PM" cell. BOD
removal in the "PM" cells was not considered in the design calculations to
predict the effluent quality, but aeration was provided to maintain aerobic
conditions in the settling ponds. In brief, the PM cells are not true partial mix
lagoons.
PERFORMANCE OF SYSTEM
Influent and effluent data are available for the NIWTP although there are
several components to the system. Because of the lack of intermediate
performance data, it is impossible to determine the influence of the
performance of the lagoon system on the final effluent quality. It is unfortunate
that intermediate data were not collected making it is impossible to determine
the efficiency of the various operations and processes. For example, it would
be beneficial to know how well the automatic backwash filters are removing
the algae from the pond effluent. All laboratory and full-scale performance
studies have shown that regular granular media filtration without chemical
addition can remove about one-third of the algae in pond effluents. The
designers expected to achieve far better results. It would be interesting to
know the basis for the design of the automatic backwash filters.
4-13
-------
Chapter 4
Extensive operating data were compiled by the staff and were made
available on computer disk for 1991 through May 1995, and this information
is shown in monthly summary reports in Appendix A. Influent and effluent flow
rates for 1991-1995 are shown in Figure 4-2. As would be expected in a
system receiving significant quantities of storm runoff, the flow rate is higher
during the rainy season (winter and spring). The influent and effluent BOD
concentrations tend to be higher during the low flow periods, and the mean
concentration has increased gradually over the past five years (Figure 4-3).
Although the mean BOD has increased with time, the mean influent TSS
concentration has tended to decrease and has become less sporadic during the
past year (Figure 4-4).
In general, the effluent fecal coliform numbers have remained essentially
constant but with occasional excursions above 200 organisms per 100 ml
(Figure 4-5). The occasional excursions probably are attributable to relatively
high TSS concentrations which interfere with the UV disinfection process.
There appeared to be no relationship between the effluent BOD
concentration and the effluent water temperature (Figures 4-6 and 4-7). This
is not surprising because of the filtration and disinfection (chlorination and
ultraviolet light) steps in the process train. Had intermediate performance data
been available, it is likely that BOD reduction would be related to temperature.
4-14
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CHAPTER 5
REYNOSA, TAMAULIPAS, MEXICO
WASTEWATER TREATMENT SYSTEM
-------
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Chapter 5
CHAPTER 5
REYNOSA, TAMAULIPAS, MEXICO WASTEWATER TREATMENT SYSTEM
The Reynosa wastewater treatment plant consists of one primary lagoon
(anaerobic) followed by five parallel facultative lagoons with three lagoons in
series. A flow diagram for the facility is shown in Figure 5-1. It was originally
planned to convert the primary lagoon into an aerated lagoon in 1992;
however, there was no aeration at the time of the site visit. Information about
the depths and volumes of the facility were not available.
The average flow rate into the system is estimated to be approximately
27 MGD which overloads the facility. The hydraulic detention time is estimated
to be less than four days with all lagoons in operation. Primary treatment is the
best that the system can deliver. The discharge requirements for the Rio
Grande/Rio Bravo of 20 mg/l of BOD and TSS cannot be met by the system.
5-1
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Chapter 5
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CHAPTER 6
OTHER UPGRADING TECHNOLOGIES
-------
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Chapter 6
CHAPTERS
OTHER UPGRADING TECHNOLOGIES
In addition to the in-pond approaches discussed in other sections there
are several innovative and alternative technologies that appear to have potential
for upgrading the effluent quality from these lagoon systems on the US-Mexico
border. These include, but are not limited to, constructed wetlands, land
application of lagoon effluent, and the use of a floating mat of duckweed plants
on some of the lagoon cells. A brief description of each of these technologies
is included below. A detailed evaluation of these and other possible
technologies is beyond the scope of this effort.
CONSTRUCTED WETLANDS
Constructed wetlands are finding increasing use for treatment and
polishing of domestic, municipal and industrial wastewaters. A recently
prepared database indicates over 1000 such systems in operation around the
world, with the majority in the United States.
There are two basic types of constructed wetlands in general use. One
type is similar to a natural marsh with emergent vegetation and with the water
surface exposed to the atmosphere; this type of wetland is called a Free Water
Surface (FWS) wetland. The other type typically uses a gravel bed up to two
feet deep with the water surface maintained below the top of the gravel. This
type is called a Subsurface Flow (SF) wetland. The same species of emergent
vegetation are used on both types of wetlands. The advantages of the SF
gravel bed type include no mosquitoes or other insect vectors, no public
exposure to the wastewater, and a higher reaction rate for pollutant removal
so a smaller sized system than FWS for the same flow rate. The disadvantage
of the SF type is the high cost of procurement and placement of the gravel
media. As a result, the SF type is generally used on smaller systems where the
advantages are critical, such as on-site home systems, parks and public
buildings, etc. The FWS concept tend to be the more economical system at
flow rates greater than 100,000 gpd, and would therefore be the likely choice
if wetlands were selected to upgrade the ponds along the border.
A FWS wetland system for any of the border sites would typically have
multiple cells in at least two parallel trains. The system could be designed for
just BOD and TSS or could also include nitrogen, phosphorus and fecal coliform
removal. For example, a wetland system designed to produce an effluent of 30
mg/l BOD (wetland influent at 50 mg/l) would require about 100 acres of
treatment area for the 37.6 MGD design flow for Mexican BCN in the year
6-1
-------
Chapter 6
2015. A wetland system designed for lower levels of BOD and/or significant
nitrogen or phosphorus removal would have to be correspondingly larger. A
wetland system at any of these border sites can be designed for optimization
of treatment or with significant habitat values for birds and other wildlife
included.
LAND APPLICATION OF LAGOON EFFLUENT
There are three basic land application technologies in use today: Slow
Rate (SR), Rapid Infiltration (Rl) and Overland Flow (OF). All three offer the
potential of very effective wastewater treatment and two of the three (SR and
OF) have the potential for beneficial crop production.
The slow rate (SR) concept is similar to normal agricultural irrigation
except in this case lagoon effluent would be used as the water source. Lagoon
effluent would be applied at a controlled rate and in amounts related to the type
of crop grown and the season of the year. A continuous year-round application
may be possible in the border region and a variety of crops would be possible.
The SR system is capable of producing very high quality water with respect to
BOD, TSS, N, P, metals, and fecal coliforms. Since crop production is an
integral part of the process the wastewater application rates are relatively low
so several thousand acres of land might be required for the 37.6 MGD flow
from Mexicali BCN in the year 2015.
The overland flow (OF) concept appears to be similar to SR, but in this
case the applied water flows over the surface of relatively impermeable soils
rather than infiltrating into the soils. The higher application rates and steeper
slopes on OF systems limit the feasible crops to forage grasses. Excellent
removal of BOD,TSS, N, metals and fecal coliforms is possible. The treated
water is collected in ditches at the toe of the slope and can be discharged or
reused. An OF system for the 2015 design flow for Mexicali BCN might require
up to 1000 acres of treatment area.
The rapid infiltration (Rl) concept depends on very high hydraulic loadings
on very permeable soils. Hydraulic loadings can range up to 2000 gallons per
square foot per year. The system usually consists of several sets of infiltration
basins which are flooded and then allowed to drain on a regular schedule.
Excellent removal of BOD, TSS, N, P, metals, and fecal coliforms are possible.
About 200 acres of Rl basins might be required for the 2015 design flow at
Mexicali BCN; however, algae which is normally present in lagoon effluents can
inhibit the infiltration rate in Rl systems and would have to be considered prior
to consideration of this concept. The presence of algae would not be a
constraint on the other land application or wetland concepts.
6-2
-------
Chapter 6
DUCKWEED COVER
Duckweed (Lemna spj is a small floating plant which can be observed
on many natural ponds, lakes, and also on wastewater treatment lagoons. The
individual plants are very small but under favorable growth conditions the plants
can form a thick mat which may then cover the entire pond surface. This mat
is very susceptible to wind forces and is typically blown to the windward side
of the pond or lagoon. If the mat of duckweed plants could be permanently
retained on the water surface then algae growth would be suppressed and
lagoon effluent quality for both BOD and TSS would be improved.
A technique for holding the duckweed plants in place is offered
commercially by the Lemna Corporation. They manufacture a set of shallow
floating baffles which are anchored to the sides of the lagoon. The baffle grid
forms cells which retain the duckweed in place on the pond. It is then
necessary to periodically harvest some of the duckweed plants, and the same
company offers a floating harvester. Both the harvester and the floating grid
are patented but the use of duckweed for this purpose is not. Application to
the lagoons on the border would probably require a duckweed mat covering
most of the existing cells to achieve desired water quality at the present flow
rates. It may also be necessary to add lagoon cells to accommodate future
design flows with this duckweed concept. The use of duckweed can improve
performance for BOD and TSS but will not provide comparable results for N and
P without extraordinary harvesting activity and/or supplemental treatment.
Because of the duckweed cover the effluent from these lagoons will be devoid
of oxygen and supplemental aeration may be required if effluent DO is a
requirement.
SYNOPSIS OF PERFORMANCE EXPECTATIONS
Tables 6-1 through 6-3 contain a synopsis of the performance
expectations for the lagoons and upgrading systems discussed in this section
of the report. A summary of the performances expected from the more
standard lagoon upgrading techniques such as intermittent sand filters, rock
filters, etc. are shown in Chapter 2 of the report.
With the selection of the proper treatment method or combination of
treatment methods, it is possible to produce a very high quality effluent that
would be acceptable for discharge to streams; groundwater recharge;
agricultural reuse; or recreational reuse in parks, golf courses, etc.
6-3
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6-6
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REFERENCES
-------
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REFERENCES
REFERENCES
AI-Layla, M.A., S. Ahmad, and E.J. Middlebrooks: Handbook of Wastewater
Collection and Treatment: Principles and Practices, Garland STPM Press New
York, NY, 1980.
Benefield, L.D., C.W. Randall: Biological Process Design for Wastewater
Treatment, Prentice-Hall, Inc., Englewood Cliffs, NJ, 1980.
Boulier, G.A., and T.J. Atchinson: "Practical Design and Application of the
Aerated-Facultative Lagoon Process," Hinde Engineering Company, Highland
Park, IL, .1975.
Canter, L.W., and A.J. Englande: "States' Design Criteria for Waste
Stabilization Ponds," J. Water Pollution Control Fed., 42(10)-1840-1847
1970. '
Engel, W.T., and T.T. Sen wing: Field Study of Nutrient Control in a Multicell
Lagoon, EPA 600/2-80-155, U.S. EPA, MERL, Cincinnati, OH, 1980.
Finney, B.A., and E.J. Middlebrooks: "Facultative Waste Stabilization Pond
Design,"J. Water Pollution Control Fed., 52(1): 134-147, 1980.
Fritz, J.J., and A.C. Middleton, D.D. Meredith: "Dynamic Process Modeling of
Waste water Stabilization Ponds, "J. Water Pollution ControlFed., 51(11)-2724-
2743, 1979.
George, R.I., "Two-dimensional Wind-generated Flow Patterns, Diffusion and
Mixing in a Shallow Stratified Pond," PhD dissertation, Utah State University
Logan, UT, 1973.
Gloyna, E.F.: "Facultative Waste Stabilization Pond Design," Ponds as a Waste
Treatment Alternative, Water Resources Symposium no. 9, University of Texas
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Gloyna, E.F. Waste Stabilization Ponds, Monograph Series No. 60, World
Health Organization, Geneva, Switzerland, 1971.
Graham, H.J., and R.B. Hunsinger: "Phosphorus Removal in Seasonal Retention
by Batch Chemical Precipitation," Project No. 71-1-1 3, Wastewater Technology
Centre, Environment Canada, Burlington, Ontario, (undated).
R-1
-------
REFERENCES
Graham, H.J., and R.B. Hunsinger: "Phosphorus Reduction from Continuous
Overflow Lagoons by Addition of Coagulants to Influent Sewage," Res. Rep.
No. 65, Ontario Ministry of the Environment, Toronto, Ontario, 1977.
Harrelson, M.E., and J.B. Cravens: "Use of Microscreens to Polish Lagoon
Effluent," J. Water Pollution Control Fed., 54(1):36-42, 1982.
Kays, W.B.: Construction of Linings for Reservoirs, Tanks, and Pollution Control
Facilities, 2nd. ed., Wiley-lnterscience Publishers, John Wiley, New York, NY,
1986.
Larson, T.B.: "A Dimensionless Design Equation for Sewage Lagoons,"
Dissertation, University of New Mexico, Albuquerque, NM, 1974.
Malina, J.F., R. Kayser, W.W. Eckenfelder, Jr., E.F. Gloyna, and W.R. Drynan:
"Design Guides for Biological Wastewater Treatment Processes," Report CRWR-
76, Center for Research in Water Resources, University of Texas, Austin,
1972.
Mancini,J.L., and E.L. Barnhart: "Industrial Waste Treatment in Aerated
Lagoons," Ponds as a Wastewater Treatment Alternative, Water Resources
Symp. No. 9, University of Texas, Austin, 1976.
Mangelson, K.A., and G.Z. Watters: "Treatment Efficiency of Waste
Stabilization Ponds," J. Sanit.Eng. Dfv., ASCE, 98(SA2), 1972.
Mangelson, K.A.: "Hydraulics of Waste Stabilization Ponds and Its Influence on
Treatment Efficiency," PhD dissertation, Utah State University, Logan, UT,
1971.
Mara, D.D.: "Discussion," Water Research, 9:595, 1975.
Marais, G.V.R.: "Dynamic Behavior of Oxidation Ponds, "Proceedings of Second
International Symposium for Waste Treatment Lagoons, Kansas City, Mo., June
23-25, 1970.
McGarry, M.C., and M.B. Pescod: "Stabilization Pond Design Criteria for
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Treatment Lagoons, Kansas City, Mo., June 23-25, 1970.
Metcalf and Eddy: Wastewater Engineering Treatment Disposal Reuse, 3rd. ed.,
McGraw Hill, New York, 1991.
R-2
-------
REFERENCES
Middlebrooks, E.J., C.H. Middlebrooks, J.H. Reynolds, G.Z. Watters, S.C.
Reed, and D.B. George: Wastewater Stabilization Lagoon Design, Performance,
and Upgrading, Macmillan, New York, 1982.
Middlebrooks, E.J., C.D. Perman, and I.S. Dunn.: Wastewater Stabilization
Pond Linings, Special Report 78-28, Cold Regions Research and Engineering
Laboratory, Hanover, NH, 1978.
Middlebrooks, E.J.: "Review of Rock Filters for the Upgrade of Lagoon
Effluents," J. Water Pollution Control Fed., 60(9): 1657-1662, 1988.
Middlebrooks, E.J.: "Design Equations for BOD Removal in Facultative
Ponds," Water Science and Technology, 19:12, 1987.
Middlebrooks, E.J., C.H. Middlebrooks, and S.C. Reed: "Energy
Requirements for Small Wastewater Treatment Systems, J. Water Pollution
Control Fed., 53: 7, 1981.
Neel, J.K., J.H. McDermott, and C.A. Monday: "Experimental Lagooning of
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Oswald, W.J., A. Meron, and M.D. Zabat: "Designing Waste Ponds to Meet
Water Quality Criteria," Proceedings of Second International Symposium for
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Pano, A., and E.J. Middlebrooks: "Ammonia Nitrogen Removal in Facultative
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Polprasert, C., and K. K. Bhattarai: "Dispersion Model for Waste Stabilization
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1984.
Reed, S.C. Wastewater Stabilization Ponds: An Update on Pathogen Removal,
Environmental Protection Agency, Office of Municipal Pollution Control,
Washington, D.C., August 1985.
Reid, L.D., Jr.: "Design and Operation for Aerated Lagoons in the Arctic and
Subarctic," Report 120, U.S. Public Health Service, Arctic Health Research
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R-3
-------
REFERENCES
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Eng. Div., ASCE, 108(EE3):532, 1982.
Russell, J.S., E.J. Middlebrooks, and J.H. Reynolds: Wastewater Stabilization
Lagoon-Intermittent Sand Filter Systems, EPA 600/2-80-032, Environmental
Protection Agency, Municipal Engineering Research Laboratory, Cincinnati, OH,
1980.
Swanson, G.R., and K.J. Williamson: "Upgrading Lagoon Effluents with Rock
Filters," J. Environ. Eng. Div., ASCE 106(EE6):1111-1119, 1980.
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Committee of Great Lakes-Upper Mississippi River Board of State Sanitary
Engineers, Health Education Services Inc., Albany, NY, 1978.
Thirumurthi, D.: "Design Criteria for Waste Stabilization Ponds," J. Water
Pollution Control Fed., 46(9):2094-2106, 1974.
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U.S. Environmental Protection Agency: Process Design Manual for Suspended
Solids Removal, EPA 625/1-75-003a, Center for Environmental Research
Information, Cincinnati, OH, 1975.
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August 1973.
U.S. Environmental Protection Agency: Process Design Manual for Upgrading
Existing Wastewater Treatment Plants, Technology Transfer,Environmental
Protection Agency, Washington, D.C., October 1974.
U.S. Environmental Protection Agency: Process Design Manual for Land
Treatment of Municipal Wastewater, EPA 625/1-81-013, Center for
Environmental Research Information, Cincinnati, OH, 1981.
U.S. Environmental Protection Agency -..Design Manual: Municipal Wastewater
Stabilization Ponds, EPA 625/1-83-015, Center for Environmental Research
Information, Cincinnati, OH, 1983.
R-4
-------
REFERENCES
U.S. Environmental Protection Agency: The 1908 Needs Survey, EPA 430/9-
81-008, Office of Water Program Operations, Washington, D.C., 1981.
U.S. Environmental Protection Agency: Design Criteria for Mechanical, Electrical
and Fluid System and Component Reliability, EPA 430/99-74-001, Office of
Water Program Operations, Washington, D.C., 1974.
Wallace, A.T.: "Land Application of Lagoon Effluents," Performance and
Upgrading of Wastewater Stabilization Ponds, EPA 600/9-79-011,
Environmental Protection Agency, Municipal Engineering Research Laboratory,
Cincinnati, OH, 1978.
Water Pollution Control Federation and American Society of Civil Engineers:
Waste water Treatment Plant Design. MOP/8, Water Pollution Control
Federation, Washington, D.C., 1977.
Wehner, J.F., R.H. Wilhelm: "Boundary Conditions of Flow Reactor," Chem.
Eng. Sc., 6:89-93, 1956.
World Health Organization: Wastewater Stabilization Pongs, Principles of
Planning & Practice, WHO Technical Publication 10, Regional Office for the
Eastern Mediterranean, Alexandria, 1987.
R-5
-------
-------
APPENDIX A
NOGALES INTERNATIONAL WASTEWATER TREATMENT PLANT
MONTHLY REPORTS
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