I
I VOLUME II: CHAPTER 5
Preferred and Alternative
Methods for Estimating Air
Emissions from Wastewater
Collection and Treatment
Final Report
March 1997
Prepared by:
Eastern Research Group
Post Office Box 2010
Morrisville, North Carolina 27560
Prepared for:
Point Sources Committee
Emission Inventory Improvement Program
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DISCLAIMER
As the Environmental Protection Agency has indicated in Emission Inventory Improvement
Program (EIIP) documents, the choice of methods to be used to estimate emissions depends on
how the estimates will be used and the degree of accuracy required. Methods using site-specific
data are preferred over other methods. These documents are non-binding guidance and not rules.
EPA, the States, and others retain the discretion to employ or to require other approaches that
meet the requirements of the applicable statutory or regulatory requirements in individual
circumstances.
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ACKNOWLEDGEMENT
This document was prepared by Mike Pring of Eastern Research Group, Inc., and Guy Fortier
of Radian International, LLC, for the Point Sources Committee, Emission Inventory
Improvement Program, and for Dennis Beauregard of the Emission Factor and Inventory
Group, U.S. Environmental Protection Agency. Members of the Point Sources Committee
contributing to the preparation of this document are:
Bill Gill, Co-Chair, Texas Natural Resource Conservation Commission
Dennis Beauregard, Co-Chair, Emission Factor and Inventory Group, U.S. Environmental Protection Agency
Denise Alston-Guiden, Galsen Corporation
Bob Betterton, South Carolina Department of Health and Environmental Control
Alice Fredlund, Louisana Department of Environmental Quality
Karla Smith Hardison, Texas Natural Resource Conservation Commission
Gary Helm, Air Quality Management, Inc.
Paul Kim, Minnesota Pollution Control Agency
Toch Mangat, Bay Area Air Quality Management District
Ralph Patterson, Wisconsin Department of Natural Resources
Jim Southerland, North Carolina Department of Environment, Health, and Natural Resources
Eitan Tsabari, Omaha Air Quality Control Division
Bob Wooten, North Carolina Department of Environment, Health, and Natural Resources
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CONTENTS
Section Page
1 Introduction 5.1-1
2 General Source Category Description 5.2-1
2.1 Source Category Description 5.2-1
2.2 Industrial WWCT Devices 5.2-1
2.2.1 Drains (Collection Unit) 5.2-1
2.2.2 Manholes (Collection Unit) 5.2-2
2.2.3 Reaches (Collection Unit) 5.2-2
2.2.4 Junction Boxes (Collection Unit) 5.2-2
2.2.5 Lift Stations (Collection Unit) 5.2-2
2.2.6 Trenches (Collection Unit) 5.2-3
2.2.7 Sumps (Collection Unit) 5.2-3
2.2.8 Weirs (Collection Unit) 5.2-3
2.2.9 Oil/Water Separators (Treatment Unit) 5.2-3
2.2.10 Equalization Basins (Treatment Unit) 5.2-4
2.2.11 Clarifiers (Treatment Unit) 5.2-4
2.2.12 Biological Treatment Basins (Treatment Unit) 5.2-4
2.2.13 Sludge Digesters (Treatment Unit) 5.2-4
2.2.14 Treatment Tanks (Treatment Unit) 5.2-5
2.2.15 Surface Impoundments (Treatment Unit) 5.2-5
2.2.16 Air and Steam Stripping (Treatment Unit) 5.2-5
2.3 Emission Sources 5.2-6
2.4 Factors and Design Considerations Influencing Emissions 5.2-8
2.4.1 Process Operating Factors 5.2-8
2.4.2 Control Techniques 5.2-9
3 Overview of Available Methods 5.3-1
3.1 Emission Estimation Methodologies 5.3-1
3.1.1 Manual Calculations 5.3-1
3.1.2 Emission Models 5.3-1
3.1.3 Gas-phase Measurement 5.3-2
3.1.4 Emission Factors 5.3-2
3.1.5 Material Balance 5.3-2
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CONTENTS (Continued)
Section Page
3.2 Comparison of Available Emission Estimation Methodologies 5.3-3
3.2.1 Manual Calculations 5.3-3
3.2.2 Emissions Models 5.3-3
3.2.3 Gas-phase Measurement 5.3-3
3.2.4 Emission Factors 5.3-4
3.2.5 Material Balance 5.3-4
4 Preferred Method for Estimating Emissions 5.4-1
4.1 WATER8/CHEMDAT8 (Treatment and Collection) 5.4-2
4.2 BASTE (Treatment Only) 5.4-2
4.3 CORAL (Collection Only) 5.4-2
4.4 PAVE (Treatment Only) 5.4-2
4.5 CINCI (EPA - Cincinnati Model) (Treatment Only) 5.4-3
4.6 NOCEPM (Treatment Only) 5.4-3
4.7 TORONTO (Treatment Only) 5.4-3
4.8 TOXCHEM+ (Treatment and Collection) 5.4-4
5 Alternative Methods for Estimating Emissions 5.5-1
5.1 Emission Factors 5.5-1
5.2 Material Balance 5.5-2
5.3 Manual Calculations 5.5-2
5.4 Gas-phase Measurement 5.5-3
5.4.1 Direct Measurement 5.5-3
5.4.2 Indirect Measurement 5.5-4
6 Quality Assurance/Quality Control 5.6-1
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CONTENTS (Continued)
Section Page
6.1 General Factors Involved in Emission Estimation
Techniques 5.6-1
6.1.1 Emissions Models 5.6-2
6.1.2 Gas-phase Measurement 5.6.2
6.1.3 Emission Factors 5.6-3
6.1.4 Material Balance 5.6-3
6.2 Data Attribute Rating System DARS Scores 5.6-3
7 References 5.7-1
Appendix A: Example Data Collection Forms - Wastewater Treatment Units
Appendix B: AP-42 Emission Estimation Algorithm and Example Calculations
Appendix C: Bibliography of Selected Available Literature on Emissions Models
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Figure and Tables
Figure Page
5.2-1 Typical Wastewater Collection and Treatment System 5.2-7
Tables Page
5.6-1 DARS Scores: Emission Models 5.6-4
5.6-2 DARS Scores: Gas-phase Measurement 5.6-4
5.6-3 DARS Scores: Emission Factors 5.6-5
5.6-4 DARS Scores: Material Balance 5.6-5
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1
Introduction
The purposes of the preferred methods guidelines are to describe emissions estimation
techniques for stationary point sources in a clear and unambiguous manner and to provide
concise example calculations to aid in the preparation of emission inventories. This chapter
describes the procedures and recommended approaches of estimating volatile organic
compound (VOC) emissions from wastewater collection and treatment (WWCT).
Section 2 of this chapter contains a general description of the WWCT source category, a
listing of common emission sources associated with WWCT, and an overview of the available
air pollution control technologies for WWCT. Section 3 of this chapter provides an overview
of available emission estimation methods. It should be noted that the use of site-specific
emissions data is always preferred over the use of industry-averaged data such as default data,
available in several of the current WWCT air emissions models. However, depending upon
available resources, obtaining site-specific data may not be cost effective. Section 4 presents
the preferred emission estimation methods for WWCT, while Section 5 presents alternative
emission estimation techniques. Quality assurance and quality control procedures are
described in Section 6, and Section 7 lists references. Appendix A contains an example data
collection form for WWCT sources, and Appendix B contains the AP-42 WWCT equations
and example calculations (Environmental Protection Agency [EPA], 1995). Appendix C
contains a list of references that may be consulted for more detailed, technical evaluations and
comparisons of the emission estimation techniques and emissions software models discussed
in this chapter.
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2
General Source Category
Description
2.1 Source Category Description
This section provides a brief overview discussion of the WWCT category. In addition to
wastewater generated at the municipal level, many industries generate large quantities of
contaminated water as a byproduct of production processes. These wastewaters typically pass
through a series of on-site collection and treatment units before discharge to a receiving water
body or publicly owned treatment works (POTW). Many of these collection and treatment
units are open to the atmosphere and allow for volatilization of VOCs from the wastewater.
The information presented in this document is applicable to any source, municipality, or
industry treating wastewater on-site.
The following sections describe the various types of wastewater collection and treatment
devices. The type of unit (collection or treatment) is provided, as is a brief description of
each. Table A-l, Appendix A lists approximate physical dimensions of several units.
2.2 WWCT Devices
2.2.1 Drains (Collection Unit)
Wastewater streams from various sources throughout a given process are normally introduced
into the collection system through process drains. Drains may be of a trapped or untrapped
design. Individual drains are usually connected directly to the main process sewer line.
However, they may also drain to trenches, sumps, or ditches. Some drains are dedicated to a
single piece of equipment such as a scrubber, decanter, or stripper. Others serve several
sources. These types of drains are located centrally between the pieces of equipment they
serve and are referred to as area drains (EPA, 1990).
2.2.2 Manholes (Collection Unit)
Manholes are service entrances into sewer lines that permit inspection and cleaning of the
sewer line. They are normally placed at periodic lengths along the sewer line. They may
also be located where sewers intersect or where there is a significant change in direction,
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grade, or sewer line diameter. The lower portion of the manhole is usually cylindrical, with a
typical inside diameter of 4 feet to allow adequate space for workers. The upper portion
tapers to the diameter of the opening at ground level. The opening is normally about 2 feet
in diameter and covered with a heavy cast-iron plate with two to four holes for ventilation
and for cover removal.
2.2.3 Reaches (Collection Unit)
A reach is a segment of sewer channel that conveys wastewater between two manholes or
other sewer components such as lift stations or junction boxes. Sanitary sewers are naturally
ventilated through holes in manhole covers, gooseneck vents (which are sometimes included
to enhance ventilation), and vent risers on buildings that are connected to sewers. (Sanitary
sewers are sometimes mechanically ventilated; i.e., fans or blowers are used to remove
hydrogen sulfide.) Combined sanitary/storm sewers are generally well-ventilated, and include
openings associated with street-level storm drains.
2.2.4 Junction Boxes (Collection Unit)
A junction box normally serves several process sewer lines. Process lines meet at the
junction box to combine the multiple wastewater streams into one stream that flows
downstream from the junction box. Liquid level in the junction box depends on the flow rate
of the wastewater. Junction boxes are either square or rectangular and are sized based on the
flow rate of the entering streams. They may also be water-sealed or covered and vented.
2.2.5 Lift Stations (Collection Unit)
Lift stations are usually the last collection unit prior to the treatment system, accepting
wastewater from one or several sewer lines. The main function of the lift station is to
provide sufficient head pressure to transport the collected wastewater to the treatment system.
A pump is used to provide the head pressure and is generally designed to operate or cut off
based on preset high and low liquid levels.
2.2.6 Trenches (Collection Unit)
Trenches are used to transport wastewater from the point of process equipment discharge to
subsequent wastewater collection units such as junction boxes and lift stations. This mode of
transport replaces the drain scenario as a method for introducing process wastewater into the
downstream collection system. In older plants, trenches are often the primary mode of
wastewater transportation in the collection system. Trenches are often interconnected
throughout the process area to accommodate pad water runoff, water from equipment washes
and spill cleanups, as well as process wastewater discharges. Normally, the length of the
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trench is determined by the general locations of the process equipment and the downstream
collection system units. This length typically ranges from 50 to 500 feet. Trench depth and
width are dictated by the wastewater flow rate discharged from process equipment. The depth
and width of the trench must be sufficient to accommodate expected as well as emergency
wastewater flows from the process equipment.
2.2.7 Sumps (Collection Unit)
Sumps are typically used for collection and equalization of wastewater flow from trenches
prior to treatment. They are usually quiescent and open to the atmosphere. Typical diameters
and depths are approximately 1.5 meters.
2.2.8 Weirs (Collection Unit)
Weirs act as dams in open channels in order to maintain constant water level upstream. The
weir face is normally aligned perpendicular to the bed and walls of the channel. Water from
the channel normally overflows the weir but may pass through a notch, or opening, in the
weir face. Because of this configuration, weirs provide some control of the level and flow
rate through the channel. This control, however, may be insignificant compared to upstream
factors that influence the supply of water to the channel.
2.2.9 Oil/Water Separators (Treatment Unit)
Oil/water separators are often the first step in the wastewater treatment plant but may also be
found in the process area. The purpose of these units is to separate liquid phases of different
specific gravities; they also serve to remove free oil and suspended solids contained in the
wastewater. Most of the separation occurs as the wastewater stream passes through a
quiescent zone in the unit. Oils and scum with specific gravities less than water float to the
top of the aqueous phase. Heavier solids sink to the bottom. Most of the organics contained
in the wastewater tend to partition to the oil phase. For this reason, most of these organic
compounds are removed with the skimmed oil leaving the separator. The wastewater stream
leaving the separator, therefore, is reduced in organic loading.
2.2.10 Equalization Basins (Treatment Unit)
Equalization basins are used to reduce fluctuations in the wastewater flow rate and organic
content to the downstream treatment processes and may be covered, stirred, or aerated.
Equalization of wastewater flow rate results in more uniform effluent quality from
downstream settling units such as clarifiers. Biological treatment performance can also
benefit significantly from the damping of concentration and flow fluctuations. This damping
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protects biological processes from upset or failure due to shock loadings of toxic or treatment-
inhibiting compounds.
2.2.11 Clarifiers (Treatment Unit)
The primary purpose of a clarifier is to separate any oils, grease, scum, and solids contained
in the wastewater. Most clarifiers are equipped with surface skimmers to clear the water of
floating oil deposits and scum. Clarifiers also have sludge raking arms that prevent
accumulation of organic solids collected at the bottom of the tank.
2.2.12 Biological Treatment Basins (Treatment Unit)
Biological waste treatment is normally accomplished through the use of aeration basins.
Microorganisms that metabolize aerobically require oxygen to carry out the biodegradation of
organic compounds that results in energy and biomass production. The aerobic environment
in the basin is normally achieved by the use of diffused or mechanical aeration. This aeration
also serves to maintain the biomass in a well-mixed regime. The goal is to maintain the
biomass concentration at a level where the treatment is efficiently optimized and proper
growth kinetics are induced.
2.2.13 Sludge Digesters (Treatment Unit)
Sludge digesters are used to treat organic sludges produced from various treatment operations.
Two types of digesters are used: anaerobic digesters and aerobic digesters.
In the anaerobic digestion process, the organic material in mixtures of primary settled and
biological sludges is converted biologically, under anaerobic conditions, to a variety of
byproducts including methane (CH4), carbon dioxide (C02), and hydrogen sulfide (H2S). The
process is carried out in an airtight reactor. Sludge, introduced continuously or intermittently,
is retained in the reactor for varying periods of time. The stabilized sludge, withdrawn
continuously or intermittently from the reactor, is reduced in organic and pathogen content
and is nonputrescible.
In aerobic digestion, the sludge is aerated for an extended period of time in an open, unheated
tank using conventional air diffusers or surface aeration equipment. The process may be
operated in a continuous or batch mode. Smaller plants use the batch system in which sludge
is aerated and completely mixed for an extended period of time, followed by quiescent
settling and decantation. In continuous systems, a separate tank is used for decantation and
concentration. High-purity oxygen aerobic digestion is a modification of the aerobic digestion
process in which high-purity oxygen is used in lieu of air. The resultant sludge is similar to
conventional aerobically digested sludge (Burton and Tchobanoglous, 1991).
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2.2.14 Treatment Tanks (Treatment Unit)
Flocculation tanks and pH adjustment tanks may be used for treatment of wastewater after
and before biological treatment, respectively. In flocculation tanks, flocculating agents are
added to the wastewater to promote formation of large-particle masses from the fine solids
formed during biological treatment. These large particles will then precipitate out of the
wastewater in the clarifier that typically follows. Tanks designed for pH adjustment typically
precede the biological treatment step. In these tanks, the wastewater pH is adjusted, using
acidic or alkaline additives, to prevent shocking of the biological system downstream.
2.2.15 Surface Impoundments (Treatment Unit)
Surface impoundments are typically used for evaporation, polishing, equalization, storage
prior to further treatment or disposal, leachate collection, and as emergency surge basins.
They may be either quiescent or mechanically agitated.
2.2.16 Air and Steam Stripping (Treatment Unit)
Air stripping and steam stripping may be used to remove organic constituents in industrial
wastewater streams prior to secondary and tertiary treatment devices.
Air stripping involves the contact of wastewater and air to strip out volatile organic
constituents. As the volume of air contacting the contaminated water increases, an increase in
the transfer rate of the organic compounds into the vapor phase is achieved. Removal
efficiencies vary with volatility and solubility of organic impurities. For highly volatile
compounds, average removal ranges from 90 to 99 percent, for medium- to low-volatility
compounds, removal ranges from less than 50 to 90 percent, though a higher air flow rate
may be needed (EPA, 1995).
Steam stripping is the distillation of wastewater to remove volatile organic constituents, with
the basic operating principle being the direct contact of steam with wastewater. The steam
provides the heat of vaporization for the more volatile organic constituents. Removal
efficiencies vary with the amount of steam applied for a given wastewater flow rate and the
volatility and solubility of the organic impurities. For highly volatile compounds (Henry's
Law constant [HLC] greater than 10~3 atm-m3/gmol), VOC removal ranges from 95 to 99
percent and can easily be achieved with a sufficient amount of steam. For medium-volatility
compounds (HLC between 10"5 and 10~3 atm-m3/gmol), average VOC removal ranges from
90 to 95 percent and would require more steam than needed for more volatile compounds.
For low-volatility compounds (HLC less than 10"5 atm-m3/gmol), average removal ranges
from less than 50 to 90 percent (EPA, 1995).
2.3 Emission Sources
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Wastewater streams are collected and treated in a variety of ways. Many of these collection
and treatment system units are open to the atmosphere and allow organic-containing
wastewaters to contact ambient air. Whenever this happens, there is a potential for VOC
emissions. The organic pollutants volatilize in an attempt to exert their equilibrium partial
pressure above the wastewater. In doing so, the organics are emitted to the ambient air
surrounding the collection and treatment units. The magnitude of VOC emissions depends
greatly on many factors such as the physical properties of the pollutants, pollutant
concentration, flow rate, the temperature of the wastewater, and the design of the individual
collection and treatment units. All of these factors, as well as the general scheme used to
collect and treat facility wastewater, have a major effect on VOC emissions.
Collection and treatment schemes are facility specific. The flow rate and organic composition
of wastewater streams at a particular facility are functions of the processes used. The
wastewater flow rate and composition, in turn, influence the sizes and types of collection and
treatment units that must be employed at a given facility.
Figure 5.2-1 illustrates a typical scheme for collecting and treating process wastewater
generated at a facility and the opportunity for volatilization of organics.
Drains are often open to the atmosphere and provide an opportunity for volatilization of
organics in the wastewater. The drain is normally connected to the process sewer line that
carries the wastewater to the downstream collection and treatment units. Figure 5.2-1
illustrates the wastewater being carried past a manhole and on to a junction box where two
process wastewater streams are joined. The manhole provides an escape route for organics
volatilized in the sewer line. In addition, the junction box may also be open to the
atmosphere, allowing organics to volatilize. Wastewater is discharged from
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PROCESS A PROCESS C
Sludge
Figure 5.2-1. Typical Wastewater Collection and Treatment System
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the junction box to a lift station where it is pumped to the treatment system. The lift station
is also likely to be open to the atmosphere, allowing volatilization of organics.
The equalization basin, the first treatment unit shown in Figure 5.2-1, regulates the
wastewater flow and pollutant compositions to the remaining treatment units. The
equalization basin also typically provides a large area for wastewater contact with ambient
air. For this reason, emissions may be relatively high from this unit. Suspended solids are
removed in the clarifier, and the wastewater then flows to the aeration basin where
microorganisms act on the organic constituents. Both the clarifier and the aeration basin may
be open to the atmosphere. In addition, the aeration basin is normally aerated either
mechanically or with diffused air. Wastewater leaving the aeration basin normally flows
through a secondary clarifier for solids removal before it is discharged from the facility. The
secondary clarifier is also likely to be open to the atmosphere. The solids that settle in the
clarifier are discharged partly to a sludge digester and partly recycled to the aeration basin.
Finally, waste sludge from the sludge digester is generally hauled off for land treatment or to
a landfill.
In addition to VOC emissions from volatilization, sulfur oxides (SOx) emissions from the
thermal destruction of hydrogen sulfide can occur if methane gas from digesters is used in on-
site combustion equipment. Chlorine and chlorinated compounds may be released if the
wastewater stream is disinfected using chlorine prior to discharge.
2.4 Factors and Design Considerations Influencing
Emissions
2.4.1 Process Operating Factors
During wastewater treatment, the fate mechanisms of volatilization/stripping, sorption, and
biotransformation primarily determine the fate of VOCs (Mihelcic et al., 1993). Of these, it
is volatilization and stripping that result in air emissions. Biodegradation and sorption onto
sludge serve to suppress air emissions.
Stripping may be defined as pollutant loss from the wastewater due to water movement
caused by mechanical agitation, head loss, or air bubbles, while volatilization may be defined
as quiescent or wind-driven loss (Mihelcic et al., 1993). The magnitude of emissions from
volatilization/stripping depends on factors such as the physical properties of the pollutants
(vapor pressure, Henry's Law constants, solubility in water, etc.), the temperature of the
wastewater, and the design of the individual collection and treatment units. WWCT unit
design is important in determining the surface area of the air-water interface and the degree of
mixing occurring in the wastewater.
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Biodegradation by microorganisms occurs in biological treatment devices such as aeration
basins. Due to the high level of biomass present in aeration basins, organic compounds may
also be removed via sorption mechanisms. Parameters important in determining the rate of
biodegradation and sorption occurring in aeration basins include the degree of
biodegradability of the compound, the affinity of the compound for the organic or aqueous
phase, and the biomass concentration in the basin (EPA, 1990). EPA has developed several
methods for determining site-specific biodegradation rates for regulatory purposes. These
include batch tests (aerated reactor and sealed reactor), as well as EPA Test Methods 304A
and 304B. However, if site-specific rate constants are not available, default biodegradation
rates are available for many pollutants in several of the emissions models used to estimate
emissions. The use of site-specific biodegradation rates will result in a more accurate
emission estimate.
Detailed information on the rates of organic removal through biodegradation, sorption, and
volatilization are required for accurate emission estimates.
2.4.2 Control Techniques
The types of control technologies generally used in reducing VOC emissions from wastewater
include: steam stripping or air stripping (when followed by a collection device such as a
carbon adsorber or a control device such as a flare), carbon adsorption (vapor or liquid
phase), chemical oxidation, biotreatment (aerobic or anaerobic), and process modifications.
Several of the control techniques (steam/air stripping and carbon adsorption) do not destroy
the VOCs, they capture them. VOCs captured by these methods should be recovered or
destroyed to prevent air emission releases to the environment.
For efficient control, all control elements should be placed as close as possible to the point of
wastewater generation, with all collection, treatment, and storage systems ahead of the control
technology being covered to suppress emissions. Tightly covered, well-maintained collection
systems can suppress emissions by 95 to 99 percent. However, if there is explosion potential,
it can be reduced by a low-volume flow of inert gas into the collection component, followed
by venting to a device such as an incinerator or carbon adsorber.
The following are brief descriptions of the control technologies listed above and of any
secondary controls that may need to be considered for fugitive air emissions.
Air and Steam Stripping
Steam stripping and air stripping off gases most often are vented to a secondary control or
collection device, such as a combustion device or gas-phase carbon adsorber, in order to
prevent air emissions. Combustion devices may include incinerators, boilers, and flares.
Vent gases of high fuel value can be used as an alternative fuel and may be combined with
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other fuels such as natural gas and fuel oil. If the fuel value of the vent gas stream is very
low, vent gases may be preheated and combined with combustion air.
Liquid-phase Carbon Adsorption
Liquid-phase carbon adsorption takes advantage of compound affinities for activated carbon.
Activated carbon is an excellent adsorbent because of its large surface area and because it is
usually in granular or powdered form for easy handling. Two types of liquid-phase carbon
adsorption are the fixed-bed and moving-bed systems. The fixed-bed system is used
primarily for low-flow wastewater streams with contact times around 15 minutes, and it is a
batch operation (i.e., once the carbon is spent, the system is taken offline). Moving-bed
carbon adsorption systems operate continuously with wastewater typically being introduced
from the bottom of the column and regenerated carbon from the top (countercurrent flow).
Spent carbon is continuously removed from the bottom of the bed. Liquid-phase carbon
adsorption is usually used to recover compounds present in low concentrations or for high
concentrations of nondegradable compounds. Removal efficiencies depend on the
compound's affinity for activated carbon. Average removal efficiency ranges from 90 to
99 percent, but is dependent on compound concentrations (EPA, 1995).
Chemical Oxidation
Chemical oxidation involves a chemical reaction between the organic compound and an
oxidant such as ozone, hydrogen peroxide, permanganate, or chlorine dioxide. Ozone is
usually added to the wastewater through an ultraviolet-ozone reactor. Permanganate and
chlorine dioxide are added directly into the wastewater. It is important to note that adding
chlorine dioxide can form chlorinated hydrocarbons in a side reaction. The applicability of
this technique depends on the reactivity of the individual organic compound.
Biotreatment
Biotreatment is the aerobic or anaerobic chemical breakdown of organic chemicals by
microorganisms. Removal of organics by biodegradation is highly dependent on the
compound's biodegradability, volatility, and ability to be adsorbed onto solids. Removal
efficiencies range from almost 0 to 100 percent. In an acclimated biotreatment system, the
microorganisms easily convert available organics into biological cells or biomass, or C02.
This often requires a mixed culture of organisms, where each organism utilizes the food
source most suitable to its metabolism. The organisms will starve and the organics will not
be biodegraded if a system is not acclimated (i.e., the organisms cannot metabolize the
available food source).
Process Modifications
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Emissions from wastewater collection or treatment units may also be reduced by process
modifications such as the use of level control gates, closed piping, or covered process units.
These techniques reduce emissions by minimizing weir drops, turbulence, and contact with
air.
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3
Overview of Available Methods
3.1 Emission Estimation Methodologies
Several methodologies are available for calculating fugitive emissions from industrial and
municipal wastewater treatment systems. The method used is dependent upon available data,
available resources, and the degree of accuracy required in the estimate.
This section discusses the methods available for calculating emissions from WWCT and
identifies the preferred method of calculation. The discussion focuses on estimating
emissions that occur from stripping mechanisms and the volatilization of pollutants present in
wastewater streams.
3.1.1 Manual Calculations
Several EPA documents are available that provide theoretical equations that may be used to
calculate emissions from WWCT. These include Industrial Wastewater Volatile Organic
Compound Emissions - Background Information for BACT/LAER Determinations
(EPA-450/3-90-004), AP-42, and Air Emissions Models for Waste and Wastewater
(EPA-453/R-94-080A). The equations are based on mass transfer and liquid-gas equilibrium
theory and use individual gas-phase and liquid-phase mass transfer coefficients to estimate
overall mass transfer coefficients. Calculating air emissions using these equations is a
complex procedure, especially if several systems are present, because the physical properties
of the numerous contaminants must be individually determined. Because of the great deal of
complexity involved, computer programs are available that incorporate these equations to
estimate emissions from WWCT.
3.1.2 Emission Models
Some emission models currently available are based on measured or empirical values. The
computer model may be based on theoretical equations that have been calibrated using actual
data. Or, the models may be purely empirical, in which case the equations are usually based
on statistical correlations with independent variables. Emissions estimated using models are a
function of the WWCT system configuration, the properties of the specific compounds present
in the wastewater streams, and the emission estimation approaches used in the model
algorithms.
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3.1.3 Gas-phase Measurement
Measuring air emissions from large open surfaces common at industrial and municipal
wastewater treatment facilities is extremely difficult and perhaps one of the most challenging
air quantification problems. Several techniques have been developed for this purpose,
including surface emission isolation flux chambers, and transect and fenceline methods. If the
industrial process is enclosed and vented, it is possible to directly measure emissions using
standard measurement techniques. (Refer to Chapter 1 of this volume for a discussion of
available methods.) In particular, POTWs may be covered or enclosed to reduce odor and/or
prevent freezing in which case gas-phase measurement may be appropriate.
3.1.4 Emission Factors
Emission factors have been or are being developed for WWCT for several source categories.
These factors have been developed as part of regulatory development projects such as the
National Emissions Standards for Hazardous Air Pollutants (NESHAP) for the pulp and paper
industry and for petroleum refineries. In some cases, emission factors are based on emissions
estimates obtained using models, but have been reduced to a more simplistic form (mass of
pollutant per process rate).
In addition, emission factors were developed by a consortium of California
POTW operators as part of the Pooled Emissions Estimation Program (PEEP). These factors
are not publicly available but may be obtained through Jim Bewley of the South Bayside
System Authority at (415) 594-8411.
The PEEP emission factors were developed from field samples at 20 POTWs and cover
18 compounds and 18 processes. Liquid- and gas-phase samples were collected to complete
mass balances at plants with similar processes. The emission factors are medians of the
measured offgas mass emissions divided by the influent mass. When no data were available,
because of "nondetects" or other causes, emission factors were extrapolated by averaging the
known emission factors of either chlorinated or nonchlorinated compounds. PEEP factors
usually predict significantly lower emissions than BAAT or fate models.
3.1.5 Material Balance
The simplest estimation method, material balance, relies on wastewater flow rate and influent
and effluent liquid-phase pollutant concentrations. Compound mass that cannot be accounted
for in the effluent is assumed to be volatilized. However, it needs to be noted that this
method does not account for biodegradation or sorption onto solids or other removal mechanisms.
3.2 Comparison of Available Emission Estimation
Methodologies
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3.2.1 Manual Calculations
Estimating emissions from WWCT by hand (or by spreadsheets) using the equations
presented in the various literature is a very labor-intensive process and increases the potential
for manual calculation error. For this reason, the use of manual calculations is not a preferred
method, and should only be used in cases where access to models is prohibitive. It should be
noted that the equations presented in the EPA document Air Emissions Model for Waste and
Wastewater (EPA, 1994) have been incorporated into EPA's WATER8 model (discussed in
Section 4) to alleviate the burden of performing the calculations by hand.
3.2.2 Emissions Models
The use of emissions software models to calculate emissions from WWCT provides a widely
accepted method of calculation. Most models are based on the theoretical equations presented
in various literature and provide an automated means of performing the calculations. It
should be noted that models estimate average emissions over a period of time. Peak or
maximum emission rates over a short term may be more accurately assessed using gas-phase
measurement or material balance approaches. Also, an in-depth knowledge of the WWCT
schemes including pollutant concentrations and flow rate information are needed in order to
obtain an accurate emission estimate.
3.2.3 Gas-phase Measurement
Direct and indirect gas-phase measurements are alternative methods of calculating emissions
from WWCT. Once pollutant concentrations are known at a specific point, atmospheric
dispersion modeling equations may be used to estimate an emission rate. Two potential
sources of uncertainty, pollutant measurement error and the representativeness of the
statistical dispersion equations for this type of application, are present in this method. In
addition, the monitoring equipment needed to perform this method may be cost-prohibitive
unless already in place.
If the treatment plant is enclosed and vented through a limited number of vents, traditional
stack testing may be used to estimate emissions and would be considered a preferred method.
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3.2.4 Emission Factors
Emission factors may be used to calculate emissions where approximate figures are
acceptable. However, due to the variability of emissions based on site-specific operational,
physical, and chemical parameters, emission factors should be carefully chosen that are based
on similar-type sources.
3.2.5 Material Balance
Material balance calculations are a simple method of estimating emissions where inlet and
outlet pollutant concentrations are known.
Other variables also may affect an estimate. Effluent data can be used to account for
compounds passing through the plant, but if chlorine is added during treatment, chlorinated
compounds that form can result in higher emissions than predicted by a material balance
approach. To compensate, intermediate samples must be taken to quantify chlorinated
compound emissions.
As mentioned before, material balance does not account for fate mechanisms other than
volatilization. For example, it can overestimate emissions if the compound is biodegradable
or adsorbs onto sludge.
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4
Preferred Method for
Estimating Emissions
The preferred method for estimating emissions from WWCT is the use of computer-
based emissions models. There are numerous emissions estimation models available to
calculate emissions from WWCT. These include publicly available models as well as
proprietary models. Differences in the models include applicability to the types of collection
and treatment systems, the level of site-specific data accepted, the level of default data
provided, and whether or not the models account for the full spectrum of pollutant pathways
(volatilization, biodegradation, and sorption). Models may also contain different default data
(e.g., Henry's Law constants, biodegradation rate constants).
Many of these models allow for user input of data. The use of site-specific data is always
preferred over the use of default data. Typically, the types of data needed are the chemical
and physical properties of the wastewater stream, as well as collection and treatment device
parameters. At a minimum, wastewater stream characteristics are needed at the inlet to the
treatment plant or collection device. However, if data are available for various points within
the treatment plant, a more accurate emissions estimate may be obtained.
In order to obtain a reliable emissions estimate using a software model, the modeler needs to
understand both the configuration and wastewater stream characteristics of the collection
and/or treatment units, as well as the emissions estimation algorithm used by the model. Not
all models can handle all collection/treatment devices and results are likely to vary between
models. A more accurate emissions estimate will result if the user has confidence in the
input data and understands the emission estimation approach used by the model.
NOTE: A brief summary of some currently available models is provided below. Work is
ongoing to improve some of the current models and to develop new ones. The discussion
presented in this document is not to be interpreted as an endorsement of one model over
another, but is provided for informational purposes only. The reader should consult with their
state regulatory agency for guidance on the selection and use of an appropriate model. Also,
Appendix C contains a reference list of technical articles providing qualitative as well as
quantitative comparisons between models and emission estimation techniques.
4.1 WATER8/CHEMDAT8 (Treatment and Collection)
WATER8 is a publicly available computer program model developed by EPA that models the
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fate of organic compounds in various wastewater treatment units, including collection
systems, aerated basins, and other units. WATER8 contains useful features such as the ability
to link treatment units to form a treatment system, the ability for recycle among units, and the
ability to generate and save site-specific compound properties. WATER8 has a database with
compound-specific data for over 950 chemicals. The mathematical equations used to
calculate emissions in this model are based on the approaches described in Air Emissions
Models for Waste and Wastewater (EPA, 1994). The WATER8 model is publicly available
on the Clearinghouse for Inventories and Emission Factors (CHIEF) system
. Many of the emissions models contained in WATER8 are also
presented in spreadsheet form in CHEMDAT8.
4.2 BASTE (Treatment Only)
This model was developed to estimate sewage treatment emissions from treatment plants in
the Bay Area of California. BASTE is a computer-based model with menu-driven input and
is structured to allow significant flexibility in simulating a wide range of treatment processes.
It can simulate the fate of organic compounds in well-mixed to plug-flow reactors, diffused
bubble and surface aeration, and emissions from weirs and drops. BASTE is available
through the CH2M Hill Company.
4.3 CORAL+ (Collection Only)
CORAL+ is a model that predicts emissions from sewer reaches based on actual data from
field experiments. CORAL+ allows for continuous or slug discharges to sewers, variations in
depth of flow and temperature, sewer physical conditions, and retardation of mass transfer by
gas accumulation in the sewer headspace. Emissions are based on inputs of ventilation rates
and patterns. CORAL+ also estimates losses at sewer drop structures and is available through
the Enviromega Ltd. Company.
4.4 PAVE (Treatment Only)
This model was developed for the Chemical Manufacturers Association. It simulates the fate
of contaminants in both surface-aerated and diffused-air activated sludge systems. The PAVE
model offers a selection of different biological kinetic models. It is based on traditional
kinetic process modelling for biological reactors and performs the traditional calculations of
dissolved oxygen concentration and waste-activated sludge flow. The PAVE model works
with compounds that have low volatilities and, therefore, may be gas-phase mass transfer
limited. Most other models use oxygen as a mass transfer surrogate so that only liquid-phase
mass transfer resistance is considered. PAVE is available through the Chemical
Manufacturers Association.
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4.5 CINCI (EPA - Cincinnati Model) - Integrated Model for
Predicting the Fate of Organics in Wastewater
Treatment Plants (Treatment Only)
This model was developed with support from the EPA Risk Reduction Engineering
Laboratory. The physical properties database of the model includes 196 chemicals and
metals, Henry's Law constants, sorption coefficients, biodegradation rate constants, and
diffusivities. Removal mechanisms included are stripping/volatilization, stripping, surface
volatilization, sorption, and biodegradation. Unit operations included are primary treatment
followed by secondary treatment with sludge recycle, secondary treatment with sludge
recycle, and secondary treatment without sludge recycle. The model is written in FORTRAN
and has three built-in default cases. CINCI is available at no charge through the U.S. EPA
Risk Reduction Engineering Laboratory.
4.6 NOCEPM - NCASI Organic Compound Elimination
Pathway Model (Treatment Only)
This model was developed by the National Council of the Paper Industry for Air and Stream
Improvement, Inc. (NCASI); components were chosen from published literature. This model
is also in the public domain. The physical properties database includes 11 chemicals, Henry's
Law constants, sorption coefficients, biodegradation rate constants, and diffusion coefficients
for 9 chemicals. Conceptual removal mechanisms are stripping, surface aeration, subsurface
aeration, surface volatilization, sorption, and biodegradation. NOCEPM simulates only the
secondary treatment step, but can represent activated sludge or aerated stabilization. It is
written in QuickBasic™ and has no built-in default cases. The model was validated with
chloroform for activated sludge and aerated stabilization processes and is available through
NCASI.
4.7 TORONTO - A Model of Organic Chemical Fate in a
Biological Wastewater Treatment Plant (Treatment
Only)
This model was developed with the support of the Ontario Ministry of the Environment, from
which copies are available. There are 18 chemicals, Henry's Law constants, sorption
coefficients, and biodegradation rate constants in the physical properties database. Removal
mechanisms include stripping, surface volatilization, sorption, and biodegradation.
TORONTO simulates primary sedimentation and secondary (biological) treatment. According
to the report, this is a relatively simple model that uses a "fugacity" approach that "takes
advantage of the linear relationship of fugacity to concentration to derive a relatively simple
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set of linear material balance expressions." Fugacity capacities and rate parameters are
calculated for the air, water, and biomass phases. TORONTO is available through the
Ontario Ministry of the Environment.
4.8 TOXCHEM+ - Toxic Chemical Modeling Program for
Water Pollution Control Plants (Treatment and
Collection)
This model was developed by Enviromega Ltd. Company (Campbellville, Ontario), in
cooperation with the Environment Canada Wastewater Technology Centre. The database
includes 204 chemicals (including metals) and detailed information on physical properties.
The model also includes Henry's Law constants, sorption coefficients, and biodegradation rate
constants. The model simulates volatilization, stripping, sorption, and biodegradation removal
mechanisms from weirs, surface volatilization, surface aeration, and subsurface aeration. A
wide variety of wastewater unit operations can be represented including grit chambers,
primary clarifiers, collection reaches, sludge digestion, aeration basins, and secondary
clarifiers. Both steady-state and dynamic results can be obtained. TOXCHEM+ is available
through the Enviromega Ltd. Company.
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5
Alternative Methods for
Estimating Emissions
5.1 Emission Factors
Emission factors for WWCT are presented in the literature in two forms: traditional emission
factors that relate emissions of a particular pollutant to a process rate, and fraction emitted
(Fe) emission factors that relate emissions of a particular pollutant to the total amount of that
pollutant present in the wastewater stream.
Examples 5.5-1 and 5.5-2 show how process rate emission factors and Fe emission factors
may be used to calculate emissions from WWCT.
Example 5.5-1
i
This example shows how toluene emissions can be calculated using Fe and the
wastewater stream characteristics provided:
Wastewater flow into
collection system =
4,575,000 gal/day
Toluene concentration =
4 |ig/L
Fe
0.35 (for the collection system)
Toluene mass flow rate =
4,575,000 gal/day * 3.785 L/gal * 4 |ig/L *
10"6 g/|ig * lb/453.6 g
0.153 lb/day
Toluene emissions =
0.35 * 0.153 lb/day
0.054 lb/day
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Example 5.5-2
i
This example shows how VOC emissions can be calculated using process rate-based
emission factors (EFs) and the process parameters provided:
EFVOC
0.17 kg VOC/Mg pulp
Process rate
= 27 Mg pulp/hr
VOC emissions
27 Mg pulp/hr * 0.17 kg VOC/Mg pulp * 1,000 g/1 kg *
lb/453.6 g
10.1 lb VOC/hr
5.2 Material Balance
Using a material balance approach to calculate emissions from WWCT is straightforward if
the data are available and if the emissions estimate does not require extreme accuracy. In
most cases, a material balance calculation will provide an emission estimate that is biased
toward overestimating emissions due to the fact that the other (nonair) pollutant removal
mechanisms (sorption and biodegradation) are not considered. This approach may be a viable
option for collection systems and nonbiologically activated treatment where inlet and outlet
pollutant concentrations are known. Example 5.5-3 shows how a material balance approach
may be used to calculate emissions from WWCT.
5.3 Manual Calculations
Appendix B provides example calculations using the mass transfer equations presented in
AP-42. The equations, along with guidance on how to use them, are included. (Please note
that while the AP-42 section still refers to the SIMS model, this has been superseded by the
WATER8 model, which is available on the CHIEF BBS. Therefore, as of the writing of this
document, AP-42 is not consistent with EPA's method of choice for estimating emissions
from wastewater treatment.)
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Example 5.5-3
i
This example shows how toluene emissions can be calculated using a material
balance approach. The wastewater stream is the same as that considered in
Example 5.5-1. However, in this example, it is known that the wastewater stream
exiting the collection system has a toluene concentration of 2 |ig/L:
Wastewater flow
=
4,575,000 gal/day
Toluene concentration at inlet
=
4 |ig/L
Toluene concentration at outlet
=
2 (ig/L
Toluene lost through system =
4 |ig/L
- 2 (ig/L = 2 (ig/L
Toluene emissions
=
4,575,000 gal/day * 3.785 L/gal *
2 ng/L * 10"6 g/|ig * lb/453.6 g
=
0.0764 lb/day
5.4 Gas-phase Measurement
5.4.1 Direct Measurement
The surface isolation flux chamber is the only commonly accepted direct measurement
technique available for open wastewater surfaces. When properly placed and operated, the
flux chamber accurately measures surface emissions. Total surface emissions are calculated
by multiplying the values from the individual flux chamber measurements by the surface area
each measurement represents. This can be quite challenging for processes that are not
completely mixed and may have unique emissions at every point on the surface. For these
cases, modeling can be used to interpolate surface emission values between flux chamber
measurement points. This method is not suitable for estimating emissions of compounds with
low volatility.
Treatment processes that are enclosed or covered may lend themselves to traditional stack
testing methods for emission estimation purposes. If a collection system or treatment plant is
well covered and vented through a limited number of openings, direct measurement (such as
the use of EPA Method 25) may be considered a preferred, rather than an alternative, method
of emission estimation.
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5.4.2 Indirect Measurement
Indirect measurement techniques, including transect and fenceline sensing, primarily are used
for estimating fugitive emissions from area sources.
Transect and fenceline methods are both indirect measurement techniques that rely on
dispersion modeling to predict the emission rate based on measurements of the ambient
pollutant concentrations in the emission plume.
The transect method typically uses both vertically and horizontally dispersed measurement
points positioned close to the source.
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6
Quality Assurance/Quality
Control
The consistent use of standardized methods and procedures is essential in the compilation of
reliable emission inventories. Quality assurance (QA) and quality control (QC) of an
inventory are accomplished through a set of procedures that ensure the quality and reliability
of data collection and analysis. These procedures include the use of appropriate emission
estimation techniques, applicable and reasonable assumptions, accuracy/logic checks of
computer models, checks of calculations, and data reliability checks. Depending upon the
technical approach used to estimate emissions, a checklist with all of the particular data needs
should be prepared to verify that each piece of information is used accurately and
appropriately.
This section discusses QA/QC procedures for specific emission estimation methods presented
in Sections 4 and 5 of this chapter. Volume VI, Quality Assurance Procedures, of this series
describes additional QA/QC methods and tools for performing these procedures. Also,
Volume II, Chapter 1, Introduction to Stationary Point Source Emission Inventory
Development, presents recommended standard procedures to follow to ensure that the reported
inventory data are complete and accurate.
6.1 General Factors Involved in Emission Estimation
Techniques
All calculations, whether done manually or electronically, should be verified by repeating at
least one complete set of calculations. If a computer model is being used, verification that
the calculations are done correctly need only be done once (until the model is updated or
modified). The model verification process should be documented carefully (see Volume VI,
Chapter 3, Section 4). Although this level of checking for a program can require a significant
amount of time, it is necessary. Furthermore, given that these programs are generally used
many times over, the effort required to check the algorithms is relatively small.
Manual calculations should be checked even more carefully, although completely replicating
the set of equations is overly burdensome. Because manual calculations introduce more
possibility for errors, are difficult to quality assure, and are harder to revise or update later,
use of a spreadsheet or other electronic tool is strongly advised.
Often, emissions inventories are developed and/or compiled in computerized emissions
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databases or models. Presumably, the methods, assumptions, and any data included with the
software are documented in a user's or a technical manual. If not, the user should conduct
extensive and careful QA of the model or find a better documented system.
Even if the validation of the system is well-documented, the user will need to provide
information about the input data. Comment fields, if available and sufficiently large, can be
used to record assumptions, data references, and any other pertinent information.
Alternatively, this information can be recorded in a separate document, electronically or
otherwise. If at all possible, the electronic database should record a cross-reference to the
document. This cross-reference could be a file name (and directory or disk number), a
notebook identification number, or other document.
6.1.1 Emissions Models
Use of emission models and equations generally involves more effort than use of emission
factors. The level of effort is related to the complexity of the equation, the types of data that
must be collected, and the diversity of products manufactured at a facility. Typically, the use
of emission models involves making one or more conservative assumptions if a complete set
of site-specific data is unavailable. As a result, the use of models may result in an
overestimation of emissions. However, the accuracy and reliability of models can be
improved by ensuring that data collected for emission calculations (e.g., material speciation
data) are of the highest possible quality.
The EIIP recommends that sensitivity analyses be used as part of the QA program for
emissions models. A sensitivity analysis is a process for identifying the magnitude, direction,
and form of the effect of an individual parameter on the model's result. It is usually done by
repeatedly running the model and changing the value of one variable while holding the others
constant. Sensitivity analyses may be used to select the most appropriate model for a given
situation. For example, one model may be particularly sensitive to errors in a variable that is
not reliably measured. An alternative model may be found that is better suited to the
available data. Sensitivity analyses also aid QC by identifying the key variables to be
checked.
6.1.2 Gas-phase Measurement
When applying this technique for estimating emissions, sampling and analytical procedures,
use of data, preparation and use of a QA plan, and report preparation should be described and
understood by the team conducting the test. A systems audit should be conducted on-site as a
qualitative review of the various aspects of a total sampling and analytical system to assess its
overall effectiveness. For detailed information pertaining to specific test methods,
procedures described in the published reference methods should be reviewed, as well as,
Chapter 1 of this volume.
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6.1.3 Emission Factors
The use of emission factors is straightforward when the relationship between process data and
emissions is direct and relatively uncomplicated. When using emission factors, the user
should be aware of the quality indicator associated with the value. Emission factors
published within EPA documents and electronic tools have a quality rating applied to them.
The lower the quality indicator, the more likely that a given emission factor may not be
representative of the source type. The reliability and uncertainty of using emission factors as
an emission estimation technique are discussed in detail in the QA/QC section of Chapter 1 of
this volume.
6.1.4 Material Balance
As stated in Section 5, the accuracy and reliability of emission values calculated using the
material balance approach are biased toward overestimation. Uncertainty of emissions using
the material balance approach is also related to the quality of material speciation data, which
is typically extracted from Material Safety Data Sheets (MSDSs). To assess the level of
uncertainty of such data, the user should verify if a standard analytical test method (e.g., one
using a gas chromatograph) has been used to measure the concentrations of the constituents.
6.2 Data Attribute Rating System (DARS) Scores
One measure of emission inventory data quality is the DARS score. Four examples are given
here to illustrate DARS scoring using the preferred and alternative methods presented in this
document. The DARS provides a numerical ranking on a scale of 0.1 to 1.0 for individual
attributes of the emission factor and the activity data. Each score is based on what is known
about the factor and activity data, such as the specificity to the source category and the
measurement technique employed. The composite attribute score for the emissions estimate
can be viewed as a statement of the confidence that can be placed in the data. For a
complete discussion of DARS and other rating systems, see the Quality Assurance Procedures
(Volume VI, Chapter 4) and Introduction to Stationary Point Sources Emission Inventory
Development (Volume II, Chapter 1).
Each of the examples below is hypothetical. A range is given where appropriate to cover
different situations. Table 5.6-1 shows scores developed from the use of emission models.
Table 5.6-2 demonstrates scores determined for gas-phase measurement. Table 5.6-3 gives a
set of scores for an estimate made with an emission factor. Table 5.6-4 demonstrates scores
developed from a material balance approach. The activity data are assumed to be measured
directly or indirectly. These examples are given as an illustration of the relative quality of
each method. If the same analysis were done for an actual site, the scores could be different
but the relative ranking of methods should stay the same.
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Table 5.6-1
DARS Scores: Emission Models
Attribute
Scores
Factor"
Activityb
Emissions
Measurement
0.3 - 0.9
1.0
0.3 - 0.9
Specificity
0.5 - 0.9
0.9
0.45 - 0.81
Spatial
1.0
1.0
1.0
Temporal
1.0
0.5 - 0.9
0.5 - 0.9
Composite Scores
0.75 - 0.95
0.85 - 0.95
0.56 - 0.90
a Lower scores apply to purely theoretical models and/or use of defaults rather than site-specific input values.
b Scores assume activity is volume of wastewater processed and that it is measured.
Table 5.6-2
DARS Scores: Gas-phase Measurement
Attribute
Scores
Factor"
Activityb
Emissions
Measurement
0.5 - 1.0
1.0
0.5 - 1.0
Specificity
0
1
©
0.9
0.63 - 0.9
Spatial
0.5 - 1.0
1.0
0.5 - 1.0
Temporal
0.5 - 1.0
0
1
©
0.35 - 1.0
Composite Scores
0.55 - 1.0
0.9 - 0.98
0.50 - 0.98
a Exact score will depend on sample size, method used, and whether scales are appropriate to inventory.
b Assumes activity is wastewater processed and measured.
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Table 5.6-3
DARS Scores: Emission Factors
Attribute
Scores
Factor
Activity"
Emissions
Measurement
0.3 - 0.5
1.0
0.3 - 0.5
Specificity
0.3 - 0.7
0.9
0.21 - 0.63
Spatial
1.0
1.0
1.0
Temporal
0.8
0.8
0.5 - 0.9
Composite Scores
0.45 - 0.85
0.78 - 0.98
0.40 - 0.76
a Scores assume activity is volume of wastewater processed and that it is measured.
Table 5.6-4
DARS Scores: Material Balance
Attribute
Scores
Factor
Activity
Emissions
Measurement51
0.5 - 0.7
1.0
0.5 - 0.7
Specificity
1.0
1.0
1.0
Spatial
1.0
1.0
1.0
Temporal13
0.5 - 1.0
0.5 - 1.0
0.25 - 1.0
Composite Scores
0.75 - 0.93
0.88 - 1.0
0.69 - 0.93
a Score increases as sample sizes (influent and effluent) increase.
b If influent/effluent concentrations are scaled up or down, lower DARS scores.
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References
Burton, F.L. and G. Tchobanoglous. 1991. Wastewater Engineering: Treatment, Disposal,
and Reuse; Metcalf & Eddy, Inc. 3rd ed. McGraw-Hill Publishing Company, New York,
New York.
EPA. 1990. Industrial Wastewater Volatile Organic Compound Emissions - Background
Information for BACT/LAER Determinations. U.S. Environmental Protection Agency,
EPA-450/3-90-004. Research Triangle Park, North Carolina.
EPA. 1992. Documentation for Developing the Initial Source Category List.
U.S. Environmental Protection Agency, EPA-450/3-91-030. Research Triangle Park,
North Carolina.
EPA. 1994. Air Emissions Models for Waste and Wastewater. U.S. Environmental
Protection Agency, EPA-453/R-94-080A. Research Triangle Park, North Carolina.
EPA. 1995. Compilation of Air Pollutant Emission Factors. Volume I: Stationary Point
and Area Sources, Fifth Edition, AP-42. U.S. Environmental Protection Agency, Office of
Air Quality Planning and Standards. Research Triangle Park, North Carolina.
Mihelcic, James R., C. Robert Baillod, John C. Crittenden, and Tony N. Rodgers.
January 1993. Estimation of VOC Emissions from Wastewater Facilities by Volatilization
and Stripping. Air & Waste, Journal of the Air & Waste Management Association. 43:
97-105.
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Appendix A
Example Data Collection
Forms-Wastewater Treatment
Units
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Example Data Collection Forms
Instructions
1. These forms may be used as work sheets to aid the plant engineer in collecting the
information necessary to calculate emissions from wastewater treatment units. The
information requested on the forms relates to the methods (described in Sections 3
through 5) for quantifying emissions. These forms may also be used by regulatory
agency personnel to assist in area-wide inventory preparation.
2. The completed forms should be maintained in a reference file by the plant engineer with
other supporting documentation.
3. If the information requested is unknown, write "unknown" in the blank. If the
information requested does not apply to a particular unit, write "NA" in the blank.
4. If you want to modify the form to better serve your needs, an electronic copy of the form
may be obtained through the EIIP on the Clearinghouse for Inventories and Emission
Factors system (CHIEF ).
5. Table A-l can be used as a reference for typical dimensions associated with each unit
design parameter.
6. Use the comments field on the form to record all useful information that will allow your
work to be reviewed and reconstructed.
EIIP Volume II
5. A-l
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CHAPTER 5 - WWCT
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Table A-1
Dimensions for Waste Stream Collection and Treatment Units3
Typical
Component
Design Parameter
Dimensions
Drain
riser height (m)
0.6
riser diameter (m)
0.2
process drain pipe diameter (m)
0.1
effective diameter of riser (m)
0.1
riser cap thickness (cm)
0.6
sewer diameter (m)
0.9
Manhole
diameter (m)
1.2
height (m)
1.2
cover diameter (m)
0.6
diameter of holes in cover (cm)
2.5
cover thickness (cm)
0.6
sewer diameter (m2)
0.9
Junction Box
effective diameter (m)
0.9
grade height (m)
1.5
water depth (m)
0.9
surface area (m2)
0.7
Lift Station
effective diameter (m)
1.5
width (m)
1.8
grade height (m)
2.1
water depth (m)
1.5
surface area (m2)
1.8
Trench
length (m)
15.2
water depth (m)
0.6
depth (m)
0.8
width (m)
0.6
Weir
height (m)
1.8
Oil/Water Separator
length (m)
13.7
width (m)
7.6
retention time (hr)
0.8
5.A-2
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Table A-1
(Continued)
Typical
Component
Design Parameter
Dimensions
Clarifier
diameter (m)
18.3
depth (m)
3.5
retention time (hr)
4.0
Sump
effective diameter (m)
1.5
water depth (m)
1.5
surface area (m2)
1.8
Equalization Basin
effective diameter (m)
109
water depth (m)
2.9
surface area (m2)
9,290
retention time (days)
5
Aeration Basin
effective diameter (m)
150
water depth (m)
2.0
surface area (m2)
17,652
retention time (days)
6.5
Treatment Tank
effective diameter (m)
11
water depth (m)
4.9
surface area (m2)
93
retention time (hr)
2
a EPA. 1990. Industrial Wastewater Volatile Organic Compound Emissions-Background Information for
BACT/LAER Determinations. U.S. Environmental Protection Agency, EPA-450/3-90-004. Research Triangle
Park, North Carolina.
EIIP Volume II
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Example Data Collection Form - Wastewater Units
GENERAL INFORMATION
Facility/Plant Name:
SIC Code:
SCC:
SCC Description:
Location:
County: City: State:
Plant Geographical Coordinates:
Latitude:
Longitude:
UTM Zone:
UTM Easting:
UTM Northing:
Contact Name:
Title:
Telephone Number:
Source ID Number:
Permit Number:
Permitted Hours of Operation (per year):
Actual Hours of Operation:
Hours/Day:
Facsimile Number:
Unit ID Number:
Days/Weeks: Weeks/Year:
5.A-4
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CHAPTER 5 - WWCT
Example Data Collection Form - Wastewater Units
UNIT DESCRIPTION3
UNIT NUMBER of
Junction box:
Reach:
Drain:
Drain type:
Lift station:
Sump:
Weir:
Other:
CONFIGURATION
Flowthrough:
Disposal:
MECHANICAL AERATION
Diffused air:
Biodegradation:
Oil film layer:
DESIGN PARAMETERS
Volume flow rate (units):
Surface area (units):
Liquid depth (units):
Width (units):
Fetch length (units):
Retention time (turnover/yr):
Pollutant of interest:
Concentration before treatment:
a Refer to Table A-l for typical dimensions associated with design parameters.
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Input Data For Modeling Wastewater Treatment Systems
COLLECTION SYSTEM
Please fill out the following information for each unit. Attach additional sheets as needed.
TRUNK/REACH
UNIT NUMBER
UNIT NUMBER
UNIT NUMBER
Wastewater flow:
Open or closed channel:
Reach (channel) diameter:
Reach surface roughness:
(e.g., smooth, concrete, tile,
pipe)
Reach slope:
Reach length:
Wastewater temperature:
Water concentration of
known organics:
Manholes and drop
structures:
Manhole gas volume:
Tailwater depth in manhole:
Air concentration of VOCs
(if available):
Water drop height in drop
structure (height of splashing
flow):
Wind speed or ventilation
rate in sewer:
5.A-6
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CHAPTER 5 - WWCT
Input Data For Modeling Wastewater Treatment Systems (Continued)
BASINS & TANKS COMMENTS
Flow rates and composition:
Influent flow rate to unit (gal/hr):
Recycle flow rate from clarifier (gal/hr):
Feed influent organics:
Major components (mg/L):
Total organics (mg/L):
Microorganism level in recycle (mg/L MLVSSa):
Microorganism level in basin (mg/L MLYSS):
Microorganism level in feed (mg/L MLVSS):
Microorganism level in clarifier effluent (mg/L MLVSS):
Oxygen concentration in feed (ppm):
Oxygen concentration in basin (ppm):
Basin geometry and characteristics:
Volume (gal):
Depth (ft):
Surface area (ft ):
Temperature of liquid in basin (°C):
Number of turbines:
Turbine speed (rpm):
Delivered power of turbine (hp/turbine):
Oxygen transfer rating of turbine (lb of Q?/hp-hr):
Diameter of turbine blade (ft):
For subsurface aeration:
Air flow to basin (ft/min):
Liquid injection rate (ft /hr):
Biodegradation rates:
Overall removal efficiency (%):
Compound-specific biorates (if known):
a MLVSS = mixed liquor volatile suspended solids.
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Ltl
00
EMISSION ESTIMATION RESULTS
c
3
CD
Pollutant
Emission
Estimation
Method*
Annual
Emissions
Emissions
Units
Emission
Factorb
Emission
Factor
Units
Comments
voc
Hazardous Air
Pollutants (list
individually)
Use the following codes to indicate which emission estimation method is used for each pollutant:
Emission Factor = EF; Other (indicate) = O; Model (indicate which model was used) = M.
Where applicable, enter the emission factor and provide the full citation of the reference or source of information from where the emission factor
came. Include edition, version, table, and page numbers if AP-42 is used.
Please copy blank form and attach additional sheets as needed.
-A.
NO
CO
VI
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CHAPTER 5 - WWCT
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Appendix B
AP-42 Emission Estimation
Algorithm and Example
Calculations
Source: EPA. January 1995. "Waste Water Collection, Treatment and Storage"
(Section 4.3.2). In: Compilation of Air Pollutant Emission Factors, Volume I: Stationary
Point and Area Sources, Fifth Edition, AP-42. U.S. Environmental Protection Agency, Office
of Air Quality Planning and Standards. Research Triangle Park, North Carolina.
Note: AP-42 refers to the SIMS model although it has been superseded by the WATER8
model, which is available on the CHIEF BBS.
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CHAPTER 5 - WWCT
Emissions
Volatile organic compounds (VOCs) are emitted from wastewater collection, treatment, and
storage systems through volatilization of organic compounds at the liquid surface. Emissions
can occur by diffusive or convective mechanisms, or both. Diffusion occurs when organic
concentrations at the water surface are much higher than ambient concentrations. The
organics volatilize or diffuse into the air, in an attempt to reach equilibrium between aqueous
and vapor phases. Convection occurs when air flows over the water surface, sweeping
organic vapors from the water surface into the air. The rate of volatilization relates directly
to the speed of the air flow over the water surface.
Other factors that can affect the rate of volatilization include wastewater surface area,
temperature, and turbulence; wastewater retention time in the system(s); the depth of the
wastewater in the system(s); the concentration of organic compounds in the wastewater and
their physical properties, such as volatility and diffusivity in water; the presence of a
mechanism that inhibits volatilization, such as an oil film; or a competing mechanism, such as
biodegradation.
The rate of volatilization can be determined by using mass transfer theory. Individual gas
phase and liquid phase mass transfer coefficients (kCT and k„, respectively) are used to
& 1 O
estimate overall mass transfer coefficients (K, Koil, and KD) for each VOC. " Figure 5.B-1
presents a flow diagram to assist in determining the appropriate emissions model for
estimating VOC emissions from various types of wastewater treatment, storage, and collection
systems. Tables 5.B-1 and 5.B-2, respectively, present the emission model equations and
definitions.
VOCs vary in their degree of volatility. The emission models presented in this section can be
used for high-, medium-, and low-volatility organic compounds. The Henry's Law constant
(HLC) is often used as a measure of a compound's volatility, or the diffusion of organics into
the air relative to diffusion through liquids. High-volatility VOCs are HLC >
10~3 atm-m3/gmol; medium-volatility VOCs are 10~3 < HLC < 10"5 atm-m3/gmol; and
low-volatility VOCs are HLC < 10 atm-mVgmol.1
The design and arrangement of collection, treatment, and storage systems are facility-specific;
therefore the most accurate wastewater emissions estimate will come from actual tests of a
facility (i.e., tracer studies or direct measurement of emissions from openings). If actual data
are unavailable, the emission models provided in this section can be used.
Emission models should be given site-specific information whenever it is available. The most
extensive characterization of an actual system will produce the most accurate
EIIP Volume II
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1,3 24
1.3 24
1,3 24
Equations Used to Obtain:®
Kj Kg Koll KD K N
1 2 7 20
12 7 19
12 7 14
12 7 13
7 16
1.3 24
2 a
2 8
2 8
2 8
3 2
7 16
18
10
5 6
8 24
Figure 5.B-1. Flow diagram for estimating VOC emissions from wastewater collection,
treatment, and storage systems.
Citation refers to table assignment number in AP-42.
5.B-2
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CHAPTER 5 - WWCT
Table 5.B-1
Mass Transfer Correlations and Emissions Equations3
Equation
No. Equation
Individual liquid (l 3.25 m/s and 14 < F/D < 51.2
kj (m/s) = (2.61 x 10-7)(U10)2(DW/Dether)2/3
For: Ujq > 3.25 m/s and F/D > 51.2
kj (m/s) = 1.0 x 10"6 + 144 x 10"4 (U*)2'2 (S^)"0'5; U* < 0.3
kj (m/s) = 1.0 x 10"6 + 34.1 x 10"4 U* (ScL)"°^; U* > 0.3
For: U10 > 3.25 m/s and F/D < 14
where:
U* (m/s) = (0.01)(U10)(6.1 + 0.63(U10))°'5
ScL = ^/(Pl^w)
F/D = 2 (A/7i)
2 kg (m/s) = (4.82 x 10-3)(U10)a78 (ScG)-°'67 (de)-° n
where:
ScG = K/'PjUj
de(m) = 2(A/u)lC
3 k, (m/s) = [<8.22 x l(T9)(J)(POWR)(l 024)(T"20)(Ot)(106) *
(MWLy(VavpL)](DII/D02iWf5
where:
POWR (hj)) = (total power to aerators)(V)
Vav(ft) = (fraction of area agitated)(A)
35
where:
k (m/s) = (1.35 x 10"7)(Re)1'42 (P)0'4 (ScG)0 5 (Fr)"0 21(Da MWa/d)
Re = d2 w pa/|ia
P = [(0.85)(POWR)(550 ft-lbf/s-hp)/Nj] gc/(pL(d*)5w3)
ScG = hAPa0Da)
Fr = (d*)w /g
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Table 5.B-1
(Continued)
Equation
No. Equation
5 kj (m/s) = (fairJ)(Q)/[3600 s/min (hc)(7idc)]
where:
fair« = 1 - 1/r
r/-» hh(\*. \0.623(r*\ /_ j /pv \0.66-i
r - exp [0.77(hc) (Q/7rdc) (Dw/D02 w) ]
6 kg (m/s) = 0.001 + (0.0462(U**)(Scg)~°-67)
where:
U** (m/s) = [6.1 + (0.63)(U10)]°-5(U10/100)
ScG = ^APaDa)
Overall mass transfer coefficients for water (K) and oil (Koil) phases and for weirs (KD)
7 K = (k^ Keq kg)/(Keq kg + 1<{)
where:
Keq = H/(RT)
8 K (m/s) = [[MWt /(k„nI *(100 cm/m)] + [MW„/(k p H*
55,555(l(So cm/m))]]"' MWL/[(100 cSi/m)pL]
^ K«il ~~ l<^Kec]01i
where:
Keq0ll = P\MWoll/(poll MWa P0)
10 Kd = 0.16h(Dtt/Do,w)1175
Air emissions (N)
11 N(g/s) = (1 - Ct/Co) V Co/t
where:
Ct/Co = exp[-K A t/V]
5.B-4
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Table 5.B-1
(Continued)
Equation
No.
Equation
12
N(g/s) = K CL A
where:
CL(g/m3) = Q Co/(KA + Q)
13
N(g/s) = (1 - Ct/Co) V Co/t
where:
Ct/Co = exp[-(KA + KeqQa)t/V]
14
N(g/s) = (KA + QaKeq)CL
where:
CL(g/m3) = QCo/(KA + Q + QaKeq)
15
N(g/s) = (1 - Ct/Co) KA/(KA + Kmax b; V/Ks) V Co/t
where:
Ct/Co = exp[-Kmax bi t/Ks - K A t/V]
16
N(g/s) = K CL A
where:
CL(g/m3) = [-b + (b2 - 4ac)°'5]/(2a)
and:
a = KA/Q + 1
b = KS(KA/Q + 1) + Kmax bx V/Q - Co
c = -KsCo
17
N(g/s) = (1 - Ctoll/Cooll)VollCooll/t
where:
CtOll/C°Oll = exP["Koil t/DOll]
and:
Cooil = Kow Co/[l - FO + FO(Kow)]
V01i = (FO)(V)
D0ll = (FO)(V)/A
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Table 5.B-1
(Continued)
Equation
No.
Equation
18
N(g/s) = Koi1CLoi1A
where:
CL,oil(§/m3) = QoilC°oil/(KoilA + Qoil)
and:
Cooil = Kow Co/[l - FO + FO(Kow)]
Q0ll = (FO)(Q)
19
N(g/s) = (1 - Ct/Co)(KA + QaKeq)/(KA + QaKeq + Kmax b; V/Ks) V Co/t
where:
Ct/Co = exp[-(KA + KeqQa)t/V - Kmax bi t/Ks]
20
N(g/s) = (KA + QaKeq)CL
where:
CL(g/m3) = [-b +(b2 - 4ac)0 5]/(2a)
and:
a = (KA + QaKeq)/Q + 1
b = KS[(KA + QaKeq)/Q + 1] + Kmax bx V/Q -
Co
c = -KsCo
21
N (g/s) = (1 - exp[-KD])Q Co
22
N(g/s) = Koi1CLoi1A
where:
CL,o,l<8/m3) = Qoi1(Cooi1*)/(Koi1A + Qoll)
and:
Cooll* = Co/FO
Q0ll = (FO)(Q)
5.B-6
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Table 5.B-1
(Continued)
Equation
No.
Equation
23
N(g/s) = (1 - Ctoll/Cooll*)(Voll)(Cooll*)/t
where:
Ctoil/C°oil* = exP["Koil t/DOll]
and:
Cooll* = Co/FO
V01i = (FO)(V)
D0ll = (FO)(V)/A
24
N (g/s) = (1 - exp[-K k dc hc/Q])Q Co
a All parameters in numbered equations are defined in Table 5.B-2.
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Table 5.B-2
Parameter Definitions for Mass Transfer Correlations
and Emissions Equations
Parameter
Definition
Units
Codea
A
Wastewater surface area
m2 or ft2
A
bi
Biomass concentration (total biological solids)
g/m3
B
cL
Concentration of constituent in the liquid phase
g/m3
D
Cuoil
Concentration of constituent in the oil phase
g/m3
D
Co
Initial concentration of constituent in the liquid
phase
g/m3
A
Cooil
Initial concentration of constituent in the oil
phase considering mass transfer resistance
between water and oil phases
g/m3
D
Cooll*
Initial concentration of constituent in the oil
phase considering no mass transfer resistance
between water and oil phases
g/m3
D
Ct
Concentration of constituent in the liquid phase
at time = t
g/m3
D
Ctoil
Concentration of constituent in the oil phase at
time = t
g/m3
D
d
Impeller diameter
cm
B
D
Wastewater depth
m or ft
A,B
d*
Impeller diameter
ft
B
Da
Diffusivity of constituent in air
cm2/s
C
dc
Clarifier diameter
m
B
de
Effective diameter
m
D
^cthcr
Diffusivity of ether in water
cm2/s
(8.5xl0"6)b
D02,w
Diffusivity of oxygen in water
cm2/s
(2.4xl0"5)b
Doil
Oil film thickness
m
B
5.B-8
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Table 5.B-2
(Continued)
Parameter
Definition
Units
Codea
Dw
Diffusivity of constituent in water
cm2/s
C
f
air,f
Fraction of constituent emitted to the air,
considering zero gas resistance
dimensionless
D
F/D
Fetch to depth ratio, de/D
dimensionless
D
FO
Fraction of volume which is oil
dimensionless
B
Fr
Froude number
dimensionless
D
§c
Gravitation constant (a conversion factor)
lbm-ft/s2-lbf
32.17
h
Weir height (distance from the wastewater
overflow to the receiving body of water)
ft
B
hc
Clarifier weir height
m
B
H
Henry's Law constant of constituent
"5
atm-m /gmol
C
J
Oxygen transfer rating of surface aerator
lb 02/(hr-hp)
B
K
Overall mass transfer coefficient for transfer of
constituent from liquid phase to gas phase
m/s
D
kd
Volatilization-reaeration theory mass transfer
coefficient
dimensionless
D
Keq
Equilibrium constant or partition coefficient
(concentration in gas phase/concentration in
liquid phase)
dimensionless
D
Kecw
Equilibrium constant or partition coefficient
(concentration in gas phase/concentration in
oil phase)
dimensionless
D
kg
Gas phase mass transfer coefficient
m/s
D
kf
Liquid phase mass transfer coefficient
m/s
D
Kmax
Maximum biorate constant
g/s-g biomass
A,C
Koil
Overall mass transfer coefficient for transfer of
constituent from oil phase to gas phase
m/s
D
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Table 5.B-2
(Continued)
Parameter
Definition
Units
Codea
Kow
Octanol-water partition coefficient
dimensionless
C
Ks
Half saturation biorate constant
g/m3
A,C
MW
d
Molecular weight of air
g/gmol
29
MW0ll
Molecular weight of oil
g/gmol
B
mwl
Molecular weight of water
g/gmol
18
N
Emissions
g/s
D
Ni
Number of aerators
dimensionless
A,B
Ot
Oxygen transfer correction factor
dimensionless
B
P
Power number
dimensionless
D
P*
Vapor pressure of the constituent
atm
C
P0
Total pressure
atm
A
POWR
Total power to aerators
hp
B
Q
Volumetric flow rate
-5
m /s
A
Qa
Diffused air flow rate
-5
m /s
B
Qoii
Volumetric flow rate of oil
-5
m /s
B
r
Deficit ratio (ratio of the difference between the
constituent concentration at solubility and
actual constituent concentration in the
upstream and the downstream)
dimensionless
D
R
Universal gas constant
-5
atm-m /gmol-K
8.21xl0"5
Re
Reynolds number
dimensionless
D
ScG
Schmidt number on gas side
dimensionless
D
ScL
Schmidt number on liquid side
dimensionless
D
5.B-10
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Table 5.B-2
(Continued)
Parameter
Definition
Units
Codea
T
Temperature of water
°C or Kelvin
(K)
A
t
Residence time of disposal
s
A
U*
Friction velocity
m/s
D
iT
Friction velocity
m/s
D
UiO
Wind speed at 10 m above the liquid surface
m/s
B
V
Wastewater volume
-5 -5
m or ft
A
Vav
Turbulent surface area
ft2
B
Voil
Volume of oil
m3
B
w
Rotational speed of impeller
rad/s
B
Pa
Density of air
-5
g/cm
(1.2xl0~3)b
Pl
Density of water
-5 -5
g/cm or lb/ft
lb or 62.4b
Poil
Density of oil
g/m3
B
Ma
Viscosity of air
g/cm-s
(1.81xl0"4)b
Ml
Viscosity of water
g/cm-s
(8.93xl0"3)b
a Code:
A = Site-specific parameter.
B = Site-specific parameter. For default values, see Table 5.B-3.
C = Parameter can be obtained from literature. See Table 5.B-4 for a list of -150 compound
chemical properties at T = 25°C (298°K).
D = Calculated value.
b Reported values at 25°C (298°K).
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estimates from an emissions model. In addition, when addressing systems involving
biodegradation, the accuracy of the predicted rate of biodegradation is improved when site-
specific compound biorates are input. Reference 3 contains information on a test method for
measuring site-specific biorates, and Table 5.B-4 presents estimated biorates for
approximately 150 compounds.
To estimate an emissions rate (N), the first step is to calculate individual gas phase and liquid
phase mass transfer coefficients kg and 1<{. These individual coefficients are then used to
calculate the overall mass transfer coefficient, K. Exceptions to this procedure are the
calculation of overall mass transfer coefficients in the oil phase, Koil, and the overall mass
transfer coefficient for a weir, KD. Koil requires only k and KD does not require any
individual mass transfer coefficients. The overall mass transfer coefficient is then used to
calculate the emissions rates. The following discussion describes how to use Figure 5.B-1 to
determine an emission rate. An example calculation is presented in Part B-l below.
Figure 5.B-l is divided into two sections: wastewater treatment and storage systems, and
wastewater collection systems. Wastewater treatment and storage systems are further
segmented into aerated/nonaerated systems, biologically active systems, oil film layer systems,
and surface impoundment flowthrough or disposal. In flowthrough systems, wastewater is
treated and discharged to a publicly owned treatment works (POTW) or a receiving body of
water, such as a river or stream. All wastewater collection systems are by definition
flowthrough. Disposal systems, on the other hand, do not discharge any wastewater.
Figure 5.B-l includes information needed to estimate air emissions from junction boxes, lift
stations, sumps, weirs, and clarifier weirs. Sumps are considered quiescent, but junction
boxes, lift stations, and weirs are turbulent in nature. Junction boxes and lift stations are
turbulent because incoming flow is normally above the water level in the component, which
creates some splashing. Wastewater falls or overflows from weirs and creates splashing in
the receiving body of water (both weir and clarifier weir models). Wastewater from weirs
can be aerated by directing it to fall over steps, usually only the weir model.
Assessing VOC emissions from drains, manholes, and trenches is also important in
determining the total wastewater facility emissions. As these sources can be open to the
atmosphere and closest to the point of wastewater generation (i.e., where water temperatures
and pollutant concentrations are greatest), emissions can be significant. Currently, there are
no well-established emission models for these collection system types. However, work is
being performed to address this need.
5.B-12
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Preliminary models of VOC emissions from waste collection system units have been
developed.4 The emission equations presented in Reference 4 are used with standard
collection system parameters to estimate the fraction of the constituents released as the
wastewater flows through each unit. The fractions released from several units are estimated
for high-, medium-, and low-volatility compounds. The units used in the estimated fractions
included open drains, manhole covers, open trench drains, and covered sumps.
The numbers in Figure 5.B-1 under the columns for k^, k Koil, KD, K, and N refer to the
appropriate equations in Table 5.B-l.a Definitions for all parameters in these equations are
given in Table 5.B-2. Table 5.B-2 also supplies the units that must be used for each
parameter, with codes to help locate input values. If the parameter is coded with the letter A,
a site-specific value is required. Code B also requires a site-specific parameter, but defaults
are available. These defaults are typical or average values and are presented by specific
system in Table 5.B-3.
Code C means the parameter can be obtained from literature data. Table 5.B-4 contains a list
of approximately 150 chemicals and their physical properties needed to calculate emissions
from wastewater, using the correlations presented in Table 5.B-1. All properties are at 25°C
(77°F). A more extensive chemical properties data base is contained in Appendix C of
Reference 1.) Parameters coded D are calculated values.
Calculating air emissions from wastewater collection, treatment, and storage systems is a
complex procedure, especially if several systems are present. Performing the calculations by
hand may result in errors and will be time consuming. A personal computer program called
the Surface Impoundment Modeling System (SIMS) is now available for estimating air
emissions. The program is menu driven and can estimate air emissions from all surface
impoundment models presented in Figure 5.B-1, individually or in series. The program
requires for each collection, treatment, or storage system component, at a minimum, the
wastewater flow rate and component surface area. All other inputs are provided as default
values. Any available site-specific information should be entered in place of these defaults,
as the most fully characterized system will provide the most accurate emissions estimate.
a All emission model systems presented in Figure 5.B-1 imply a completely mixed or uniform waste
water concentration system. Emission models for a plug flow system, or system in which there is no
axial, or horizontal mixing, are too extensive to be covered in this document. (An example of plug
flow might be a high waste water flow in a narrow channel.) For information on emission models
of this type, see Reference 1.
EIIP Volume II
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CHAPTER 5 - WWCT
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Table 5.B-3
Site-Specific Default Parameters3
Default
Parameter*1
Definition
Default Value
General
T
Temperature of water
298°K
Uio
Windspeed
4.47 m/s
Biotreatment Systems
bi
Biomass concentration (for biologically active
systems)
Quiescent treatment systems
50 g/m3
Aerated treatment systems
300 g/m3
Activated sludge units
4000 g/m3
POWR
Total power to aerators
(for aerated treatment systems)
(for activated sludge)
0.75 hp/1000 ft3 (V)
2 hp/1000 ft3 (V)
W
Rotational speed of impeller
(for aerated treatment systems)
126 rad/s (1200 rpm)
*
d(d)
Impeller diameter
(for aerated treatment systems)
61 cm (2 ft)
Vav
Turbulent surface area
(for aerated treatment systems)
(for activated sludge)
0.24 (A)
0.52 (A)
J
Oxygen transfer rating to surface aerator
(for aerated treatment systems)
3 lb 02/hp*hr
Ot
Oxygen transfer correction factor
(for aerated treatment systems)
0.83
Ni
Number of aerators
POWR/75
Diffused Air Systems
Qa
Diffused air volumetric flow rate
0.0004(V) m3/s
5.B-14
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CHAPTER 5 - WWCT
Table 5.B-3
(Continued)
Default
Parameter*1
Definition
Default Value
Oil Film Layers
MW0ll
Molecular weight of oil
282 g/gmol
Doil
Depth of oil layer
0.001 (V/A) m
V01l
Volume of oil
0.001 (V) m3
Qoii
Volumetric flow rate of oil
0.001 (Q) m3/s
Poil
Density of oil
0.92 g/cm3
FO
Fraction of volume which is oilc
0.001
Junction Boxes
D
Depth of Junction Box
0.9 m
N:
Number of aerators
1
Lift Station
D
Depth of Lift Station
1.5 m
N:
Number of aerators
1
Sump
D
Depth of sump
5.9 m
Weirs
dc
Clarifier weir diameter01
28.5 m
h
Weir height
1.8 m
hc
Clarifier weir height6
0.1 m
Reference 1.
As defined in Table 5.B-2.
Reference 4.
Reference 2.
Reference 5.
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CHAPTER 5 - WWCT
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The SIMS program with user's manual and background technical document can be obtained
through state air pollution control agencies and through the U.S. Environmental Protection
Agency's Control Technology Center in Research Triangle Park, North Carolina, telephone
(919) 541-0800. The user's manual and background technical document should be followed
to produce meaningful results.
The SIMS program and user's manual also can be downloaded from EPA's Clearinghouse for
Inventories and Emission Factors system (CHIEF ). The CHIEF is
open to all persons involved in air emission inventories.
First-time users must register before access is
allowed.
Emissions estimates from SIMS are based on mass transfer models developed by Emissions
Standards Division (ESD) during evaluations of treatment, storage, and disposal facilities
(TSDFs) and VOC emissions from industrial wastewater. As a part of the TSDF project, a
Lotus® spreadsheet program called CHEMDAT7 was developed for estimating VOC
emissions from wastewater land treatment systems, open landfills, closed landfills, and waste
storage piles, as well as from various types of surface impoundments. For more information
about CHEMDAT7, contact the ESD's Chemicals And Petroleum Branch (MD-13), U.S.
Environmental Protection Agency, Research Triangle Park, North Carolina 27711.
Example Calculation
An example industrial facility operates a flowthrough, mechanically aerated biological
treatment impoundment that receives wastewater contaminated with benzene at a
concentration of 10.29 g/m .
The following format is used for calculating benzene emissions from the treatment process:
I. Determine which emission model to use
II. User-supplied information
III. Defaults
IV. Pollutant physical property data and water, air, and other properties
V. Calculate individual mass transfer coefficient
VI. Calculate the overall mass transfer coefficients
VII. Calculate VOC emissions
I. Determine Which Emission Model To Use — Following the flow diagram in Figure 5.B-1,
5.B-16
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CHAPTER 5 - WWCT
the emission model for a treatment system that is aerated, but not by diffused air, is
biologically active, and is a flowthrough system, contains the following equations:
Equation Nos.
Parameter Definition from Table 5.B-1
K Overall mass transfer coefficient, m/s 7
l<{ Individual liquid phase mass transfer coefficient, m/s 1,3
kg Individual gas phase mass transfer coefficient, m/s 2, 4
N VOC emissions, g/s 16
II. User-supplied Information — Once the correct emission model is determined, some site-
specific parameters are required. As a minimum for this model, site-specific flow rate,
wastewater surface area and depth, and pollutant concentration should be provided. For
this example, these parameters have the following values:
Q = Volumetric flow rate = 0.0623 m3/s
D = Wastewater depth = 1.97 m
'j
A = Wastewater surface area = 17,652 m
Co = Initial benzene concentration in the liquid phase = 10.29 g/m
III. Defaults — Defaults for some emission model parameters are presented in Table 5.B-3.
Generally, site-specific values should be used when available. For this facility, all
available general and biotreatment system defaults from Table 5.B-3 were used:
Ujo = Wind speed at 10 m above the liquid surface = e = 4.47 m/s
T = Temperature of water = 25°C (298°K)
bi = Biomass concentration for aerated treatment systems = 300 g/m3
J = Oxygen transfer rating to surface aerator = 3 lb 02/hp-hr
POWR = Total power to aerators = 0.75 hp/1,000 ft3 (V)
Ot = Oxygen transfer correction factor = 0.83
Vav = Turbulent surface area = 0.24 (A)
d = Impeller diameter = 61 cm
d = Impeller diameter = 2 ft
w = Rotational speed of impeller =126 rad/s
Nj = Number of aerators = POWR/75 hp
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IV. Pollutant Physical Property Data, And Water, Air and Other Properties — For each
pollutant, the specific physical properties needed by this model are listed in Table 5.B-4.
Water, air, and other property values are given in Table 5.B-2.
A. Benzene (from Table 5.B-4)
Dw benzene = Diffusivity of benzene in water = 9.8 x 10"6 cm2/s
Da benzene = Diffusivity of benzene in air = 0.088 cm2/s
benzene = Henry's Law constant for benzene = 0.0055 atm- m3/gmol
Kmaxbenzene = Maximum biorate constant for benzene = 5.28 x 10"6
Ks benzene = Half saturation biorate constant for benzene =13.6 g/m
B. Water, Air, and Other Properties (from Table 5.B-2)
pa = Density of air = 1.2 x 103 g/cm3
pL = Density of water = 1 g/cm (62.4 lbm/ft3)
|ia = Viscosity of air = 1.81 x 10 g/cm-s
D02w = Diffusivity of oxygen in water = 2.4 x 10"5 cm2/s
Dether = Diffusivity of ether in water = 8.5 x 10"6 cm2/s
MWl = Molecular weight of water =18 g/gmol
MWa = Molecular weight of air = 29 g/gmol
gc = Gravitation constant = 32.17 lbm-ft/lb|-s2
R = Universal gas constant = 8.21 x 10"5 atm-m3/gmol
V. Calculate Individual Mass Transfer Coefficients — Because part of the impoundment is
turbulent and part is quiescent, individual mass transfer coefficients are determined for
both turbulent and quiescent areas of the surface impoundment.
Turbulent area of impoundment — Equations 3 and 4 from Table 5.B-1.
A. Calculate the individual liquid mass transfer coefficient, 1<{:
k/m/s) = [(8.22 x 10"9)(J)(POWR)(1.024)(T"20) *
(Ot)(106)MWL/(VavpL)](Dw/DO2w)a5
The total power to the aerators, POWR, and the turbulent surface area, Vav, are
calculated separately [Note: some conversions are necessary.]:
1. Calculate total power to aerators, POWR (Default presented in III):
POWR (hp) = 0.75 hp/1,000 ft3 (V)
V = wastewater volume, m
V (m3) = (A)(D) = (17,652 m2)(1.97 m)
V = 34,774 m3
POWR = (0.75 hp/1,000 ft3)(ft3/0.028317 m3)(34,774 m3)
= 921 hp
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CHAPTER 5 - WWCT
2. Calculate turbulent surface area, Vav (default presented in III):
Vav (ft2) = 0.24 (A)
= 0.24(17,652 m2)(10.758 ft2/m2)
= 45,576 ft2
Now, calculate k^, using the above calculations and information from II, III, and IV:
(m/s) = [(8.22 x 10"9)(3 lb 02/hp-hr)(921 hp) *
(1.024)(25"20)(0.83)(106)(18 g/gmol)/
((45,576 ft2)(l g/cm3))] *
[(9.8 x 10"6 cm /s)/(2.4 x 10"5 cm2/s)]0 5
= (0.00838)(0.639)
k^ = 5.35 x 10~3 m/s
B. Calculate the individual gas phase mass transfer coefficient, kg:
kg (m/s) = (1.35 x 10-7)(Re)L42(P)0-4(ScG)0-5(Fr)-°-21(Da MWa/d)
The Reynolds number, Re, power number, P, Schmidt number on the gas side, ScG,
and Froude's number, Fr, are calculated separately:
1. Calculate Reynolds number, Re:
Re = d2 w pa/|ia
= (61 cm)2(126 rad/s)(1.2 x 10"3 g/cm3)/(1.81 x 10~4 g/cm-s)
= 3.1 x 106
2. Calculate power number, P:
P = [(0.85)(POWR)(550 ft-lbf/s-hp)/NI] gc/(pL(d*)5 w3)
Nj = POWR/75 hp (default presented in III)
P = (0.85)(75 hp)(POWR/POWR)(550 ft-lb/s-hp) *
(32.17 lb -ft/lbrs2)/[(62.4 lbm/ft3)(2 ft)5(126 rad/s)3]
= 2.8 x 104
3. Calculate Schmidt number on the gas side, ScG:
ScG = |ia/(paDa)
= (1.81 x 10"4 g/cm-s)/[(1.2 x 10"3 g/cm3)(0.088 cm2/s)]
= 1.71
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4. Calculate Froude number, Fr:
Fr = (d*)w2/gc
= (2 ft)(126 rad/s)2/(32.17 lbm-ft/lbrs2)
= 990
Now, calculate k using the above calculations and information from II, III, and IV:
o
k (m/s) = (1.35 x 10"7)(3.1 x 106)L42(2.8 x 10~4)a4(1.71)a5 *
(990)"°'21(0.088 cm2/s)(29 g/gmol)/(61 cm)
= 0.109 m/s
Quiescent surface area of impoundment — Equations 1 and 2 from Table 5.B-1.
A. Calculate the individual liquid phase mass transfer coefficient, 1<{:
F/D = 2(A/7T)°-5/D
= 2(17,652 m2/7t)°'5/(1.97 m)
= 76.1
= 4.47
For U10 > 3.25 m/s and F/D > 51.2 use the following:
U10 = 4.47 m/s
k, (m/s) = (2.61 x 10-0(U10)Z(D /Dethery
= (2.61 x 10 )(4.47 m/s) [(9.8 x 10 cm /s)/
(8.5 x 10"6 cm2/s)]2/3
= 5.74 x 10"6 m/s
B. Calculate the individual gas phase mass transfer coefficient, kCT:
kg = (4 82 xlO-3)(U10)a78(ScG)-a«(de)-°'"
The Schmidt number on the gas side, ScG, and the effective diameter, de, are
calculated separately:
1. Calculate the Schmidt number on the gas side, ScG:
ScG = |ia/(paDa) = 1.71 (same as for turbulent impoundments)
2. Calculate the effective diameter, de:
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CHAPTER 5 - WWCT
de (m) = 2(AJ%f5
= 2(17,652 m2/7T)0-5
= 149.9 m
k (m/s) = (4.82 x 10"3)(4.47 m/s)078 (1.71)"0 67 (149.9 m)"011
= 6.24 x 10~3 m/s
VI. Calculate The Overall Mass Transfer Coefficient — Because part of the impoundment is
turbulent and part is quiescent, the overall mass transfer coefficient is determined as an
area-weighted average of the turbulent and quiescent overall mass transfer coefficients.
(Equation 7 from Table 5.B-1).
Overall mass transfer coefficient for the turbulent surface area of impoundment. KT
Kt (m/s) = (k^Keqk )/(Keqk + 1<{)
Keq = H/RT
= (0.0055 atm-m3/gmol)/[(8.21 x 10"5 atm-m3/ gmol-°K)
(298°K)]
= 0.225
Kt (m/s) = (5.35 x 10"3 m/s)(0.225)(0.109)/[(0.109 m/s)(0.225) +
(5.35 x 10"6 m/s)]
Kt = 4.39 x 10"3 m/s
Overall mass transfer coefficient for the quiescent surface area of impoundment Kq
Kq (m/s) = (k^Keqk )/(Keqk + 1<{)
= (5.74 x 10"6 m/s)(0.225)(6.24 x 10"3 m/s)/
[(6.24 X 10"3 m/s)(0.225) + (5.74 x 10"6 m/s)]
= 5.72 x 10"6 m/s
Overall mass transfer coefficient K, weighted by turbulent and quiescent surface areas,
At and Aq
K (m/s) = (KtAt + KqAq)/A
At = 0.24(A) (Default value presented in III: AT = Vav)
AQ = (1 - 0.24)A
K (m/s) = [(4.39 x 10"3 m/s)(0.24 A) + (5.72 x 10"6 m/s)
(1 - 0.24)A]/A
= 1.06 x 10"3 m/s
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VII. Calculate VOC Emissions For An Aerated Biological Flowthrough Impoundment —
Equation 16 from Table 5.B-1:
N (g/s) = K CL A
where:
CL (g/m3) = [-b + (b2 - 4ac)0 5]/(2a)
and:
a = KA/Q + 1
b = KS(KA/Q + 1) + Kmax bx V/Q - Co
c = -KsCo
Calculate a, b, c, and the concentration of benzene in the liquid phase, CL, separately:
1. Calculate a:
a = (KA/Q + 1) = [(1.06 x 10"3 m/s)(17,652 m2)/(0.0623 m3/s)] + 1
= 301.3
2. Calculate b (V = 34,774 m3 from IV):
b = Ks (KA/Q + 1) + Kmax bx V/Q - Co
= (13.6 g/m3)[(1.06 x 10"3 m/s)(17,652 m2)/(0.0623 m3/s)] +
[(5.28 x 10"6 g/g-s)(300 g/m3)(34,774 m3)/(0.0623 m3/s)] - 10.29 g/m3
= 4,084.6 + 884.1 - 10.29
= 4,958.46 g/m3
3. Calculate c:
c = -KsCo
= -(13.6 g/m3)(10.29 g/m3)
= -139.94
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CHAPTER 5 - WWCT
4. Calculate the concentration of benzene in the liquid phase, CL, from a, b, and c
above:
CL (g/m3) = [-b + (b2 - 4ac)0 5]/(2a)
= [(4,958.46 g/m3) + [(4,958.46 g/m3)2 -
[4(301.3)(-139.94)]]°'5]/(2(301.3))
= 0.0282 g/m3
Now calculate N with the above calculations and information from II and V:
N (g/s) = KACl
= (1.06 x 10"3 m/s)(17,652 m2)(0.0282 g/m3)
= 0.52 g/s
Glossary of Terms
Basin - an earthen or concrete-lined depression used to hold liquid.
Completely mixed - having the same characteristics and quality throughout or at all times.
Disposal - the act of permanent storage. Flow of liquid into, but not out of a
device.
Drain -
a device used for the collection of liquid. It may be open to the
atmosphere or be equipped with a seal to prevent emissions of vapors.
Flowthrough - having a continuous flow into and out of a device.
Plug flow -
having characteristics and quality not uniform throughout. These will
change in the direction the fluid flows, but not perpendicular to the
direction of flow (i.e., no axial movement).
Storage -
any device to accept and retain a fluid for the purpose of future
discharge. Discontinuity of flow of liquid into and out of a device.
Treatment -
the act of improving fluid properties by physical means. The removal
of undesirable impurities from a fluid.
voc -
volatile organic compounds, referring to all organic compounds except
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CHAPTER 5 - WWCT
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the following, which have been shown not to be photochemically
reactive: methane, ethane, trichlorotrifluoroethane, methylene chloride,
1,1,1 ,-trichloroethane, trichlorofluoromethane, dichlorodifluoromethane,
chlorodifluoromethane, trifluoromethane, dichlorotetrafluoroethane, and
chl oropentafluoroethane.
5.B-24
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Table 5.B-4
Sims Chemical Property Data File (Part 1)
Chemical Name
CAS
Number
Molecular
Weight
Vapor Pressure
At 25°C
(mm Hg)
Henry's Law
Constant At 25°C
(atm-m3/mol)
Diffusivity Of
Chemical In
Water
At 25°C
(cm2/s)
Diffusivity Of
Chemical In
Air At 25°C
(cm2/s)
ACETALDEHYDE
75-07-0
44.00
760
0.000095
0.0000141
0.124
ACETIC ACID
64-19-7
60.05
15.4
0.0627
0.000012
0.113
ACETIC ANHYDRIDE
108-24-7
102.09
5.29
0.00000591
0.00000933
0.235
ACETONE
67-64-1
58.00
266
0.000025
0.0000114
0.124
ACET ONITRILE
75-05-8
41.03
90
0.0000058
0.0000166
0.128
ACROLEIN
107-02-8
56.10
244.2
0.0000566
0.0000122
0.105
ACRYL AMIDE
79-06-1
71.09
0.012
0.00000000052
0.0000106
0.097
ACRYLIC ACID
79-10-7
72.10
5.2
0.0000001
0.0000106
0.098
ACRYLONITRILE
107-13-1
53.10
114
0.000088
0.0000134
0.122
ADIPIC ACID
124-04-9
146.14
0.0000225
0.00000000005
0.00000684
0.0659
ALLYL ALCOHOL
107-18-6
58.10
23.3
0.000018
0.0000114
0.114
AMINOPHENOL(-O)
95-55-6
109.12
0.511
0.00000367
0.00000864
0.0774
AMINOPHENOL(-P)
123-30-8
109.12
0.893
0.0000197
0.00000239
0.0774
AMMONIA
7664-41-7
17.03
7470
0.000328
0.0000693
0.259
AMYL ACETATE(-N)
628-37-8
130.18
5.42
0.000464
0.0000012
0.064
ANILINE
62-53-3
93.10
1
0.0000026
0.0000083
0.07
BENZENE
71-43-2
78.10
95.2
0.0055
0.0000098
0.088
BENZO(A)ANTHRACENE
56-55-3
228.30
0.00000015
0.00000000138
0.000009
0.051
BENZO(A)PYRENE
50-32-8
252.30
0.00568
0.00000000138
0.000009
0.043
-------
Table 5.B-4 (Part 1)
(Continued)
Chemical Name
CAS Number
Molecular
Weight
Vapor Pressure
At 25°C
(mm Hg)
Henry's Law
Constant At 25°C
(atmm3/mol)
Diffusivity Of
Chemical In
Water
At 25°C
(cm2/s)
Diffusivity Of
Chemical In
Air At 25°C
(cm2/s)
CRESYLIC ACID
1319-77-3
108.00
0.3
0.0000017
0.0000083
0.074
CROTONALDEHYDE
4170-30-0
70.09
30
0.00000154
0.0000102
0.0903
CUMENE (ISOPROPYLBENZENE)
98-82-8
120.20
4.6
0.0146
0.0000071
0.065
CYCLOHEXANE
110-82-7
84.20
100
0.0137
0.0000091
0.0839
CYCLOHEXANOL
108-93-0
100.20
1.22
0.00000447
0.00000831
0.214
CYCLOHEXANONE
108-94-1
98.20
4.8
0.00000413
0.00000862
0.0784
DI-N-OCTYL PHTHALATE
117-84-0
390.62
0
0.137
0.0000041
0.0409
DIBUTYLPHTHALATE
84-74-2
278.30
0.00001
0.00000028
0.0000079
0.0438
DICHLORO(-2)BUTENE(l ,4)
764-41-0
125.00
2.87
0.000259
0.00000812
0.0725
DICHLOROBENZENE( 1,2) (-O)
95-50-1
147.00
1.5
0.00194
0.0000079
0.069
DICHLOROBENZENE(l,3) (-M)
541-73-1
147.00
2.28
0.00361
0.0000079
0.069
DICHLOROBENZENE( 1,4) (-P)
106-46-7
147.00
1.2
0.0016
0.0000079
0.069
DICHLORODIFLUOROMETHANE
75-71-8
120.92
5000
0.401
0.00001
0.0001
DICHLOROETHANE( 1,1)
75-34-3
99.00
234
0.00554
0.0000105
0.0914
DICHLOROETHANE( 1,2)
107-06-2
99.00
80
0.0012
0.0000099
0.104
DICHLOROETHYLENE( 1,2)
156-54-2
96.94
200
0.0319
0.000011
0.0935
DICHLOROPHENOL(2,4)
120-83-2
163.01
0.1
0.0000048
0.0000076
0.0709
DICHLOROPHENOXYACETIC ACID(2,4)
94-75-7
221.00
290
0.0621
0.00000649
0.0588
DICHLOROPROPANE( 1,2)
78-87-5
112.99
40
0.0023
0.0000087
0.0782
CO
-A.
NO
CO
VI
-------
Table B-4 (Part 1)
(Continued)
CO
Chemical Name
CAS Number
Molecular
Weight
Vapor Pressure
At 25°C
(mm Hg)
Henry's Law
Constant At 25°C
(atmm3/mol)
Diffusivity Of
Chemical In
Water
At 25°C
(cm2/s)
Diffusivity Of
Chemical In
Air At 25 °C
(cm2/s)
DIETHYL (N,N) ANILINE
91-66-7
149.23
0.00283
0.0000000574
0.00000587
0.0513
DIETHYL PHTHALATE
84-66-2
222.00
0.003589
0.0111
0.0000058
0.0542
DIMETHYL FORMAMIDE
68-12-2
73.09
4
0.0000192
0.0000103
0.0939
DIMETHYL HYDRAZINE/1,1)
57-14-7
60.10
157
0.000124
0.0000109
0.106
DIMETHYL PHTHALATE
131-11-3
194.20
0.000187
0.00000215
0.0000063
0.0568
DIMETHYLBENZ(A)ANTHRACENE
57-97-6
256.33
0
0.00000000027
0.00000498
0.0461
DIMETHYLPHENOL(2,4)
105-67-9
122.16
0.0573
0.000921
0.0000084
0.0712
DINITROBENZENE (-M)
99-65-0
168.10
0.05
0.000022
0.00000764
0.279
DINITROTOLUENE(2,4)
121-14-2
182.10
0.0051
0.00000407
0.00000706
0.203
DIOXANE(l,4)
123-91-1
88.20
37
0.0000231
0.0000102
0.229
DIOXIN
NOCAS2
322.00
0
0.0000812
0.0000056
0.104
DIPHENYL AMINE
122-39-4
169.20
0.00375
0.00000278
0.00000631
0.058
EPICHLOROHYDRIN
106-89-8
92.50
17
0.0000323
0.0000098
0.086
ETHANOL
64-17-5
46.10
50
0.0000303
0.000013
0.123
ETHANOLAMINE(MONO-)
141-43-5
61.09
0.4
0.000000322
0.0000114
0.107
ETHYL ACRYLATE
140-88-5
100.00
40
0.00035
0.0000086
0.077
ETHYL CHLORIDE
75-00-3
64.52
1200
0.014
0.0000115
0.271
ETHYL-(2)PROPYL-(3) ACROLEIN
645-62-5
92.50
17
0.0000323
0.0000098
0.086
ETHYLACETATE
141-78-6
88.10
100
0.000128
0.00000966
0.0732
c5
-------
Table 5.B-4 (Part 1)
(Continued)
Chemical Name
CAS Number
Molecular
Weight
Vapor Pressure
At 25°C
(mm Hg)
Henry's Law
Constant At 25°C
(atmm3/mol)
Diffusivity Of
Chemical In
Water
At 25 °C
(cm2/s)
Diffusivity Of
Chemical In
Air At 25°C
(cm2/s)
ETHYLBENZENE
100-41-4
106.20
10
0.00644
0.0000078
0.075
ETHYLENEOXIDE
75-21-8
44.00
1250
0.000142
0.0000145
0.104
ETHYLETHER
60-29-7
74.10
520
0.00068
0.0000093
0.074
FORMALDEHYDE
50-00-0
30.00
3500
0.0000576
0.0000198
0.178
FORMIC ACID
64-18-6
46.00
42
0.0000007
0.00000137
0.079
FREONS
NOCAS3
120.92
5000
0.401
0.00001
0.104
FURAN
110-00-9
68.08
596
0.00534
0.0000122
0.104
FURFURAL
96-01-1
96.09
2
0.0000811
0.0000104
0.0872
HEPTANE (ISO)
142-82-5
100.21
66
1.836
0.00000711
0.187
HEXACHLOROBENZENE
118-74-1
284.80
1
0.00068
0.00000591
0.0542
HEXACHLOROBUTADIENE
87-68-3
260.80
0.15
0.0256
0.0000062
0.0561
HEXACHLOROC Y CLOPENTADIENE
77-47-4
272.80
0.081
0.016
0.00000616
0.0561
HEXACHLOROETHANE
67-72-1
237.00
0.65
0.00000249
0.0000068
0.00249
HEXANE(-N)
100-54-3
86.20
150
0.122
0.00000777
0.2
HEXANOL(-l)
111-27-3
102.18
0.812
0.0000182
0.00000753
0.059
HYDROCYANIC ACID
74-90-8
27.00
726
0.000000465
0.0000182
0.197
HYDROFLUORIC ACID
7664-39-3
20.00
900
0.000237
0.000033
0.388
HYDROGEN SULFIDE
7783-06-4
34.10
15200
0.023
0.0000161
0.176
ISOPHORONE
78-59-1
138.21
0.439
0.00000576
0.00000676
0.0623
-------
Table 5.B-4 (Part 1)
(Continued)
CO
Chemical Name
CAS Number
Molecular
Weight
Vapor Pressure
At 25°C
(mm Hg)
Henry's Law
Constant At 25°C
(atmm3/mol)
Diffusivity Of
Chemical In
Water
At 25°C
(cm2/s)
Diffusivity Of
Chemical In
Air At 25 °C
(cm2/s)
METHANOL
67-56-1
32.00
114
0.0000027
0.0000164
0.15
METHYL ACETATE
79-20-9
74.10
235
0.000102
0.00001
0.104
METHYL CHLORIDE
74-87-3
50.50
3830
0.00814
0.0000065
0.126
METHYL ETHYL KETONE
78-93-3
72.10
100
0.0000435
0.0000098
0.0808
METHYL ISOBUTYL KETONE
108-10-1
100.20
15.7
0.0000495
0.0000078
0.075
METHYL METHACRYLATE
80-62-6
100.10
39
0.000066
0.0000086
0.077
METHYL STYRENE (ALPHA)
98-83-9
118.00
0.076
0.00591
0.0000114
0.264
METHYLENE CHLORIDE
75-09-2
85.00
438
0.00319
0.0000117
0.101
MORPHOLINE
110-91-8
87.12
10
0.0000573
0.0000096
0.091
NAPHTHALENE
91-20-3
128.20
0.23
0.00118
0.0000075
0.059
NITROANILINE(-O)
88-74-4
138.14
0.003
0.0000005
0.000008
0.073
NITROBENZENE
98-95-3
123.10
0.3
0.0000131
0.0000086
0.076
PENTACHLOROBENZENE
608-93-5
250.34
0.0046
0.0073
0.0000063
0.057
PENTACHLOROETHANE
76-01-7
202.30
4.4
0.021
0.0000073
0.066
PENTACHLOROPHENOL
87-86-5
266.40
0.00099
0.0000028
0.0000061
0.056
PHENOL
108-95-2
94.10
0.34
0.000000454
0.0000091
0.082
PHOSGENE
75-44-5
98.92
1390
0.171
0.00000112
0.108
PHTHALIC ACID
100-21-0
166.14
121
0.0132
0.0000068
0.064
PHTHALIC ANHYDRIDE
85-44-9
148.10
0.0015
0.0000009
0.0000086
0.071
C5
-------
Table 5.B-4 (Part 1)
(Continued)
Chemical Name
CAS Number
Molecular
Weight
Vapor Pressure
At 25°C
(mm Hg)
Henry's Law
Constant At 25°C
(atmm3/mol)
Diffusivity Of
Chemical In
Water
At 25°C
(cm2/s)
Diffusivity Of
Chemical In
Air At 25 °C
(cm2/s)
PICOLINE(-2)
108-99-6
93.12
10.4
0.000127
0.0000096
0.075
POLY CHLORINATED BIPHENYLS
1336-36-3
290.00
0.00185
0.0004
0.00001
0.104
PROPANOL (ISO)
71-23-8
60.09
42.8
0.00015
0.0000104
0.098
PROPIONALDEHYDE
123-38-6
58.08
300
0.00115
0.0000114
0.102
PROPYLENE GLYCOL
57-55-6
76.11
0.3
0.0000015
0.0000102
0.093
PROPYLENE OXIDE
75-66-9
58.10
525
0.00134
0.00001
0.104
PYRIDINE
110-86-1
79.10
20
0.0000236
0.0000076
0.091
RESORCINOL
108-46-3
110.11
0.00026
0.0000000188
0.0000087
0.078
STYRENE
100-42-5
104.20
7.3
0.00261
0.000008
0.071
TETRACHLOROETHANE( 1,1,1,2)
630-20-6
167.85
6.5
0.002
0.0000079
0.071
TETRACHLOROETHANE(l ,1,2,2)
79-34-5
167.85
6.5
0.00038
0.0000079
0.071
TETRACHLOROETHYLENE
127-18-4
165.83
19
0.029
0.0000082
0.072
TETRAHYDROFURAN
109-99-9
72.12
72.1
0.000049
0.0000105
0.098
TOLUENE
109-88-3
92.40
30
0.00668
0.0000086
0.087
TOLUENE DIISOCYANATE(2,4)
584-84-9
174.16
0.08
0.0000083
0.0000062
0.061
TRICHLORO(l ,1,2)TRIFLUOROETHANE
76-13-1
187.38
300
0.435
0.0000082
0.078
TRICHLOROBENZENE( 1,2,4)
120-82-1
181.50
0.18
0.00142
0.0000077
0.0676
TRICHLOROBUTANE( 1,2,3)
NOCAS5
161.46
4.39
4.66
0.0000072
0.066
TRICHLOROETHANE( 1,1,1)
71-55-6
133.40
123
0.00492
0.0000088
0.078
CO
-A.
NO
CO
VI
-------
Table 5.B-4 (Part 1)
(Continued)
Chemical Name
CAS
Number
Molecular
Weight
Vapor Pressure
At 25°C
(mm Hg)
Henry's Law
Constant At 25 °C
(atmm3/mol)
Diffusivity Of
Chemical In
Water
At 25°C
(cm2/s)
Diffusivity Of
Chemical In
Air At 25°C
(cm2/s)
TRICHLOROETHANE( 1,1,2)
79-00-5
133.40
25
0.000742
0.0000088
0.078
TRICHLOROETHYLENE
79-01-6
131.40
75
0.0091
0.0000091
0.079
TRICHLOROFLUOROMETHANE
75-69-4
137.40
796
0.0583
0.0000097
0.087
TRICHLOROPHENOL(2,4,6)
88-06-2
197.46
0.0073
0.0000177
0.0000075
0.0661
TRICHLOROPROPANE( 1,1,1)
NOCAS6
147.43
3.1
0.029
0.0000079
0.071
TRICHLOROPROPANE( 1,2,3)
96-18-4
147.43
3
0.028
0.0000079
0.071
UREA
57-13-6
60.06
6.69
0.000264
0.0000137
0.122
VINYL ACETATE
108-05-4
86.09
115
0.00062
0.0000092
0.085
VINYL CHLORIDE
75-01-4
62.50
2660
0.086
0.0000123
0.106
VINYLIDENE CHLORIDE
75-35-4
97.00
591
0.015
0.0000104
0.09
XYLENE(-M)
1330-20-7
106.17
8
0.0052
0.0000078
0.07
XYLENE(-O)
95-47-6
106.17
7
0.00527
0.00001
0.087
-------
Table 5.B-4
Sims Chemical Property Data File (Part 2)
Chemical Name
Antoine's
Equation Vapor
Pressure
Coefficient
A
Antoine's
Equation Vapor
Pressure
Coefficient
B
Antoine's
Equation Vapor
Pressure
Coefficient
C
Maximum
Biodegradation
Rate Constant
(g/g Biomass-s)
Half Saturation
Constant
(g/m3)
Octanol-Water
Partition
Coefficient
At 25°C
ACETALDEHYDE
8.005
1600.017
291.809
0.0000228944
419.0542
2.69153
ACETIC ACID
7.387
1533.313
222.309
0.0000038889
14.2857
0.48978
ACETIC ANHYDRIDE
7.149
1444.718
199.817
0.0000026944
1.9323
1
ACETONE
7.117
1210.595
229.664
0.0000003611
1.1304
0.57544
ACET ONITRILE
7.119
1314.4
230
0.00000425
152.6014
0.45709
ACROLEIN
2.39
0
0
0.0000021667
22.9412
0.81283
ACRYL AMIDE
11.2932
3939.877
273.16
0.00000425
56.2388
6.32182
ACRYLIC ACID
5.652
648.629
154.683
0.0000026944
54.7819
2.04174
ACRYLONITRILE
7.038
1232.53
222.47
0.000005
24
0.12023
ADIPIC ACID
0
0
0
0.0000026944
66.9943
1.20226
ALLYL ALCOHOL
0
0
0
0.0000048872
3.9241
1.47911
AMINOPHENOL(-O)
0
0
0
0.00000425
68.1356
3.81533
AMINOPHENOL(-P)
-3.357
699.157
-331.343
0.00000425
68.1356
3.81533
AMMONIA
7.5547
1002.711
247.885
0.00000425
15.3
1
AMYL ACETATE(-N)
0
0
0
0.0000026944
16.1142
51.10801
ANILINE
7.32
1731.515
206.049
0.0000019722
0.3381
7.94328
BENZENE
6.905
1211.033
220.79
0.0000052778
13.5714
141.25375
BENZO(A)ANTHRACENE
6.9824
2426.6
156.6
0.0000086389
1.7006
407380.2778
CO
-A.
NO
CO
VI
-------
Table 5.B-4 (Part 2)
(Continued)
Chemical Name
Antoine's
Equation Vapor
Pressure
Coefficient
A
Antoine's
Equation
Vapor Pressure
Coefficient
B
Antoine's
Equation Vapor
Pressure
Coefficient
C
Maximum
Biodegradation
Rate Constant
(g/g Biomass-s)
Half Saturation
Constant
(g/m3)
Octanol-Water
Partition
Coefficient
At 25°C
BENZO(A)PYRENE
9.2455
3724.363
273.16
0.0000086389
1.2303
954992.58602
BENZYL CHLORIDE
0
0
0
0.0000049306
17.5674
199.52623
BIS(2-CHLOROETHYL)ETHER
0
0
0
0.0000029889
20.0021
38.01894
BIS(2-CHLOROISOPROPYL)ETHER
0
0
0
0.0000029889
8.3382
380.1894
BIS(2-ETHYLHEXYL)PHTHALATE
0
0
0
0.0000002139
2.2
199526.2315
BROMOFORM
0
0
0
0.0000029889
10.653
199.52623
BROMOMETHANE
0
0
0
0.0000029889
30.4422
12.58925
BUTADIENE-(1,3)
6.849
930.546
238.854
0.0000042534
15.3
74.32347
BUTANOL (ISO)
7.4743
1314.19
186.55
0.0000021667
70.9091
5.62341
BUTANOL-(l)
7.4768
1362.39
178.77
0.0000021667
70.9091
5.62341
BUTYL BENZYL PHTHALATE
0
0
0
0.0000086389
14.1364
60255.95861
CARBON DISULFIDE
6.942
1169.11
241.59
0.0000042534
5.8175
1
CARBON TETRACHLORIDE
6.934
1242.43
230
0.0000004167
1
524.80746
CHLORO(-P)CRESOL(-M)
0
0
0
0.0000029889
5.2902
1258.92541
CHLOROACETALDEHYDE
0
0
0
0.0000029889
49.838
3.4405
CHLOROBENZENE
6.978
1431.05
217.55
0.0000001083
.039
316.22777
CHLOROFORM
6.493
929.44
196.03
0.0000008167
3.7215
91.20108
CHLORONAPHTHALENE-(2)
0
0
0
0.0000029889
2.167
13182.56739
-------
Table 5.B-4 (Part 2)
(Continued)
Chemical Name
Antoine's
Equation Vapor
Pressure
Coefficient
A
Antoine's
Equation
Vapor Pressure
Coefficient
B
Antoine's
Equation Vapor
Pressure
Coefficient
C
Maximum
Biodegradation
Rate Constant
(g/g Biomass-s)
Half
Saturation
Constant
(g/m3)
Octanol-Water
Partition
Coefficient
At 25°C
CHLOROPRENE
6.161
783.45
179.7
0.0000029968
6.3412
1
CRESOL(-M)
7.508
1856.36
199.07
0.0000064472
1.3653
93.32543
CRESOL(-O)
6.911
1435.5
165.16
0.0000063278
1.34
95.49926
CRESOL(-P)
7.035
1511.08
161.85
0.0000064472
1.3653
87.09636
CRESYLIC ACID
0
0
0
0.0000041667
15
1
CROTONALDEHYDE
0
0
0
0.0000026944
27.6285
12.36833
CUMENE (ISOPROPYLBENZENE)
6.963
1460.793
207.78
0.0000086458
16.5426
1
CYCLOHEXANE
6.841
1201.53
222.65
0.0000042534
15.3
338.0687
CYCLOHEXANOL
6.255
912.87
109.13
0.0000026944
18.0816
37.74314
CYCLOHEXANONE
7.8492
2137.192
273.16
0.0000031917
41.8921
6.45654
DI-N-OCTYL PHTHALATE
0
0
0
0.000000083
0.02
141253.7
DIBUTYLPHTHALATE
6.639
1744.2
113.59
0.0000001111
0.4
158489.31925
DICHLORO(-2)BUTENE(l ,4)
0
0
0
0.0000029889
9.8973
242.1542
DICHLOROBENZENE( 1,2) (-O)
0.176
0
0
0.0000006944
4.3103
2398.83292
DICHLOROBENZENE(l,3) (-M)
0
0
0
0.0000017778
2.7826
2398.83292
DICHLOROBENZENE( 1,4) (-P)
0.079
0
0
0.0000017778
2.7826
2454.70892
DICHLORODIFLUOROMETHANE
0
0
0
0.0000029889
12.0413
144.54398
DICHLOROETHANE( 1,1)
0
0
0
0.0000029889
4.6783
61.6595
DICHLOROETHANE( 1,2)
7.025
1272.3
222.9
0.0000005833
2.1429
61.6595
-------
rn
Table 5.B-4 (Part 2)
(Continued)
Chemical Name
Antoine's
Equation Vapor
Pressure
Coefficient
A
Antoine's
Equation
Vapor Pressure
Coefficient
B
Antoine's
Equation Vapor
Pressure
Coefficient
C
Maximum
Biodegradation
Rate Constant
(g/g Biomass-s)
Half
Saturation
Constant
(g/m3)
Octanol-Water
Partition
Coefficient
At 25°C
DICHLOROETHYLENE( 1,2)
6.965
1141.9
231.9
0.0000029889
6.3294
1
DICHLOROPHENOL(2,4)
0
0
0
0.0000069444
7.5758
562.34133
DICHLOROPHENOXYACETIC ACID(2,4)
0
0
0
0.0000029889
14.8934
82.61445
DICHLOROPROPANE( 1,2)
6.98
1380.1
22.8
0.0000047222
12.1429
1
DIETHYL (N,N) ANILINE
7.466
1993.57
218.5
0.00000425
27.0047
43.57596
DIETHYL PHTHALATE
0
0
0
0.000000753
1.28
1412.537
DIMETHYL FORMAMIDE
6.928
1400.87
196.43
0.00000425
15.3
1
DIMETHYL HYDRAZINE/1,1)
7.408
1305.91
225.53
0.00000425
15.3
1
DIMETHYL PHTHALATE
4.522
700.31
51.42
0.0000006111
0.7097
74.13102
DIMETHYLBENZ(A)ANTHRACENE
0
0
0
0.0000086389
0.3377
28680056.33087
DIMETHYLPHENOL(2,4)
0
0
0
0.0000029722
2.2766
263.0268
DINITROBENZENE (-M)
4.337
229.2
-137
0.00000425
29.9146
33.28818
DINITROTOLUENE(2,4)
5.798
1118
61.8
0.00000425
19.5233
102.3293
DIOXANE(l,4)
7.431
1554.68
240.34
0.0000026944
24.7001
16.60956
DIOXIN
12.88
6465.5
273
0.0000029968
6.3412
1
DIPHENYL AMINE
0
0
0
0.0000052778
8.4103
1659.58691
EPICHLOROHYDRIN
8.2294
2086.816
273.16
0.0000029968
6.3412
1.07152
ETHANOL
8.321
1718.21
237.52
0.0000024444
9.7778
0.47863
ETHANOLAMINE(MONO-)
7.456
1577.67
173.37
0.00000425
223.0321
0.16865
CO
-A.
NO
CO
VI
0
5
~D
01
'td
LtJ
c5
-------
Table 5.B-4 (Part 2)
(Continued)
Chemical Name
Antoine's
Equation Vapor
Pressure
Coefficient
A
Antoine's
Equation
Vapor Pressure
Coefficient
B
Antoine's
Equation Vapor
Pressure
Coefficient
C
Maximum
Biodegradation
Rate Constant
(g/g Biomass-s)
Half
Saturation
Constant
(g/m3)
Octanol-Water
Partition
Coefficient
At 25°C
ETHYL ACRYLATE
7.9645
1897.011
273.16
0.0000026944
39.4119
4.85667
ETHYL CHLORIDE
6.986
1030.01
238.61
0.0000029889
22.8074
26.91535
ETHYL-(2)PROPYL-(3) ACROLEIN
0
0
0
0.000004425
15.3
1
ETHYLACETATE
7.101
1244.95
217.88
0.0000048833
17.58
1
ETHYT/BENZENE
6.975
1424.255
213.21
0.0000018889
3.2381
1412.53754
ETHYLENEOXIDE
7.128
1054.54
237.76
0.0000011667
4.6154
0.50003
ETHYLETHER
6.92
1064.07
228.8
0.0000026944
17.1206
43.57596
FORMALDEHYDE
7.195
970.6
244.1
0.0000013889
20
87.09636
FORMIC ACID
7.581
1699.2
260.7
0.0000026944
6.3412
0.1191
FREONS
0
0
0
0.0000029968
6.3412
1
FURAN
6.975
1060.87
227.74
0.0000026944
14.1936
71.37186
FURFURAL
6.575
1198.7
162.8
0.0000026944
18.0602
37.86047
HEPTANE (ISO)
6.8994
1331.53
212.41
0.0000042534
15.3
1453.372
HEXACHLOROBENZENE
0
0
0
0.0000029889
0.6651
295120.92267
HEXACHLOROBUTADIENE
- 0.824
0
0
0.000003
6.3412
5495.408
HEXACHLOROC Y CLOPENTADIENE
0
0
0
0.0000029968
0.3412
9772.372
HEXACHLOROETHANE
0
0
0
0.0000029889
3.3876
4068.32838
HEXANE(-N)
6.876
1171.17
224.41
0.0000042534
15.3
534.0845
HEXANOL(-l)
7.86
1761.26
196.66
0.0000026944
15.2068
59.52851
-------
rn
Table 5.B-4 (Part 2)
(Continued)
Chemical Name
Antoine's
Equation Vapor
Pressure
Coefficient
A
Antoine's
Equation
Vapor Pressure
Coefficient
B
Antoine's
Equation Vapor
Pressure
Coefficient
C
Maximum
Biodegradation
Rate Constant
(g/g Biomass-s)
Half
Saturation
Constant
(g/m3)
Octanol-Water
Partition
Coefficient
At 25°C
HYDROCYANIC ACID
7.528
1329.5
260.4
0.0000026944
1.9323
1
HYDROFLUORIC ACID
7.217
1268.37
273.87
0.0000026944
1.9323
1
HYDROGEN SULFIDE
7.614
885.319
250.25
0.0000029889
6.3294
1
ISOPHORONE
0
0
0
0.00000425
25.6087
50.11872
METHANOL
7.897
1474.08
229.13
0.000005
90
0.19953
METHYL ACETATE
7.065
1157.63
219.73
0.0000055194
159.2466
0.81285
METHYL CHLORIDE
7.093
948.58
249.34
0.0000029889
14.855
83.17638
METHYL ETHYL KETONE
6.9742
1209.6
216
0.0000005556
10
1.90546
METHYL ISOBUTYL KETONE
6.672
1168.4
191.9
0.0000002056
1.6383
23.98833
METHYL METHACRYLATE
8.409
2050.5
274.4
0.0000026944
109.2342
0.33221
METHYL STYRENE (ALPHA)
6.923
1486.88
202.4
0.0000008639
11.12438
2907.589
METHYLENE CHLORIDE
7.409
1325.9
252.6
0.0000061111
54.5762
17.78279
MORPHOLINE
7.7181
1745.8
235
0.00000425
291.9847
0.08318
NAPHTHALENE
7.01
1733.71
201.86
0.0000117972
42.47
1
NITROANILINE(-O)
8.868
336.5
273.16
0.00000425
22.8535
67.6083
NITROBENZENE
7.115
1746.6
201.8
0.0000030556
4.7826
69.1831
PENTACHLOROBENZENE
0
0
0
0.0000029889
0.4307
925887.02902
PENTACHLOROETHANE
6.74
1378
197
0.0000029889
0.4307
925887.02902
PENTACHLOROPHENOL
0
0
0
0.0000361111
38.2353
102329.29923
CO
-A.
NO
CO
VI
0
5
~D
01
'td
LtJ
^1
c5
-------
Table 5.B-4 (Part 2)
(Continued)
Chemical Name
Antoine's
Equation Vapor
Pressure
Coefficient
A
Antoine's
Equation
Vapor Pressure
Coefficient
B
Antoine's
Equation Vapor
Pressure
Coefficient
C
Maximum
Biodegradation
Rate Constant
(g/g Biomass-s)
Half
Saturation
Constant
(g/m3)
Octanol-Water
Partition
Coefficient
At 25°C
PHENOL
7.133
1516.79
174.95
0.0000269444
7.4615
28.84032
PHOSGENE
6.842
941.25
230
0.00000425
70.8664
3.4405
PHTHALIC ACID
0
0
0
0.0000026944
34.983
6.64623
PHTHALIC ANHYDRIDE
8.022
2868.5
273.16
0.0000048872
3.9241
0.23988
PICOLINE(-2)
7.032
1415.73
211.63
0.00000425
44.8286
11.48154
POLYCYLORINATED BIPHENYLS
0
0
0
0.000005278
20
1
PROPANOL (ISO)
8.117
1580.92
219.61
0.0000041667
200
0.69183
PROPIONALDEHYDE
16.2315
2659.02
-44.15
0.0000026944
39.2284
4.91668
PROPYLENE GLYCOL
8.2082
2085.9
203.5396
0.0000026944
109.3574
0.33141
PROPYLENE OXIDE
8.2768
1656.884
273.16
0.0000048872
3.9241
1
PYRIDINE
7.041
1374.8
214.98
0.0000097306
146.9139
4.4684
RESORCINOL
6.9243
1884.547
186.0596
0.0000026944
35.6809
6.30957
STYRENE
7.14
1574.51
224.09
0.0000086389
282.7273
1445.43977
TETRACHLOROETHANE(l ,1,2)
6.898
1365.88
209.74
0.0000029889
6.3294
1
TETRACHLOROETHANE(l ,1,2,2)
6.631
1228.1
179.9
0.0000017222
9.1176
363.07805
TETRACHLOROETHYLENE
6.98
1386.92
217.53
0.0000017222
9.1176
398.10717
TETRAHYDROFURAN
6.995
1202.29
226.25
0.0000026944
20.3702
27.58221
TOLUENE
6.954
1344.8
219.48
0.0000204111
30.6167
489.77882
TOLUENE DIISOCYANATE(2,4)
0
0
0
0.0000425
15.3
1
-------
rn
c
3
CD
Table 5.B-4 (Part 2)
(Continued)
Chemical Name
Antoine's
Equation Vapor
Pressure
Coefficient
A
Antoine's
Equation
Vapor Pressure
Coefficient
B
Antoine's
Equation Vapor
Pressure
Coefficient
C
Maximum
Biodegradation
Rate Constant
(g/g Biomass-s)
Half
Saturation
Constant
(g/m3)
Octanol-Water
Partition
Coefficient
At 25°C
TRICHLORO( 1,1,2)TRIFLUOROETHANE
6.88
1099.9
227.5
0.0000029889
3.3876
4068.32838
TRICHLOROBENZENE( 1,2,4)
0
0
0
0.0000029889
2.4495
9549.92586
TRICHLOROBUTANE( 1,2,3)
0
0
0
0.0000029968
6.3412
1450901.06626
TRICHLOROETHANE( 1,1,1)
8.643
2136.6
302.8
0.0000009722
4.7297
309.02954
TRICHLOROETHANE(l ,1,2)
6.951
1314.41
209.2
0.0000009722
4.7297
1
TRICHLOROETHYLENE
6.518
1018.6
192.7
0.0000010833
4.4318
194.98446
TRICHLOROFLUOROMETHANE
6.884
1043.004
236.88
0.000003
6.3412
338.8441
TRICHLOROPHENOL(2,4,6)
0
0
0
0.0000425
58.8462
4897.78819
TRICHLOROPROPANE( 1,1,1)
0
0
0
0.0000029889
10.7719
193.7827
TRICHLOROPROPANE( 1,2,3)
6.903
788.2
243.23
0.0000029889
10.7719
193.7827
UREA
0
0
0
0.00000425
4.8169
4068.32838
VINYL ACETATE
7.21
1296.13
226.66
0.0000026944
31.8363
8.51722
VINYL CHLORIDE
3.425
0
0
0.000003
6.3412
1.14815
VINYLIDENE CHLORIDE
6.972
1099.4
237.2
0.0000029968
6.3412
1
XYLENE(-M)
7.009
1426.266
215.11
0.0000086389
14.0094
1584.89319
XYLENE(-O)
6.998
1474.679
213.69
0.0000113306
22.8569
891.25094
CO
-A.
NO
CO
VI
0
5
~D
01
'td
LtJ
VO
C5
-------
CHAPTER 5 - WWCT
3/12/97
References
1. Hazardous Waste Treatment, Storage, and Disposal Facilities (TSDF)-Air Emission
Models, EPA-450/3-87-026, U.S. Environmental Protection Agency, Research Triangle
Park, NC, April 1989.
2. Wastewater Treatment Compound Property Processor Air Emissions Estimator
(WATER 7), U.S. Environmental Protection Agency, Research Triangle Park, NC,
available early 1992.
3. Evaluation of Test Method for Measuring Biodegradation Rates of Volatile Organics,
Draft, EPA Contract No. 68-D90055, Entropy Environmental, Research Triangle Park,
NC, September 1989.
4. Industrial Wastewater Volatile Organic Compound Emissions-Background Information
for BACT/LAER Determinations, EPA-450/3-90-004, U.S. Environmental Protection
Agency, Research Triangle Park, NC, January 1990.
5. Evan K. Nyer, Ground Water Treatment Technology, Van Nostrand Reinhold
Company, New York, 1985.
5.B-40
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CHAPTER 5 - WWCT
Appendix C
Bibliography of Selected
Available Literature on
Emissions Models
EIIP Volume II
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CHAPTER 5 - WWCT
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CHAPTER 5 - WWCT
Card, T.R. 1995. Comparison of Mass Transfer Models with Direct Measurement for Free
Liquid Surfaces at Wastewater Treatment Facilities. Presented at the 88th Annual AWMA
Meeting, San Antonio, Texas. June 18-23.
Card, T.R., and P. Benson. 1992. Modeling the Air Emissions from an Industrial Wastewater
Treatment Facility. Presented at the 1992 AWMA Convention, Kansas City, Missouri.
June 21-26.
Corsi, R.L. 1989. Volatile Organic Compound Emissions from Wastewater Collection
Systems. Dissertation. University of California, Davis.
Corsi, R.L., and C.J. Quigley. 1995. "VOC emissions from sewer junction boxes and drop
structures: Estimation of methods and experimental results." In: Proceedings of the 88th
Annual Meeting of the Air & Waste Management Association. Air & Waste Management
Association, Pittsburgh, Pennsylvania.
Ferro, A. and A.B. Pincince. 1996. Comparison of Computer Programs for Estimating
Emissions of Volatile Organic Compounds from Wastewater Treatment Facilities.
Proceedings of the Water Environment Federation 69th Annual Conference and Exposition,
Dallas, Texas, October 5-9.
Jones, D.L., J.W. Jones, J.C. Seaman, R.L. Corsi, and C.F. Burklin. 1996. Models to
Estimate Volatile Organic Hazardous Air Pollutant Emissions from Municipal Sewer Systems.
Journal of the Air & Waste Management Association 46:657.
Pincince, A.B. and A. Ferro. 1996. Estimating VOC Emissions from Primary Clarifiers.
Water Environment & Technology 8(6):47.
Schroy, J.S. 1994. Estimation of Emissions from Wastewater Treatment Systems: A
Comparison of Available Software Performance. Paper and Session ID, presented at the
AIChE 1994 Summer National Meeting, "VOC and Air Toxics Emissions - Estimating and
Control," August 15, 1994.
Tata, P., S. Solszynski, D.P. Lordi, D.R. Zenz, C. Lue-Hign. 1994. Volatile Organic
Compound Emissions from the Water Reclamation Plants of the Metropolitan Water
Reclamation District of Greater Chicago. Presented at the Odor and Volatile Organic
Compound Emission Control for Municipal and Industrial Treatment Facilities Conference,
Jacksonville, Florida. April.
EIIP Volume II
5.C-1
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CHAPTER 5 - WWCT
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Tata, P., S. Solszynski, D.P. Lordi, D.R. Zenz, C. Lue-Hign. 1995. Prediction of Volatile
Organic Compound Emissions from Publicly Owned Treatment Works. Presented at the 68th
Annual WEFTEC Meeting, Miami Beach, Florida. October.
Thompson, D., J. Bell, L. Sterne, and P. Jann. 1996. Comparing Organic Contaminant
Emission Estimates Using "WATER8" and "TOXCHEM+". Proceedings of the Water
Environment Federation 69th Annual Conference and Exposition, Dallas, Texas, October 5-9.
5.C-2
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