United States
Environmental Protection
Agency
Office of Air Quality
Planning and Standards
Research Triangle Par|
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EPA-450/2-90-009
LOCATING AND ESTIMATING
AIR TOXICS EMISSIONS FROM
SEWAGE SLUDGE INCINERATORS
By
Radian Corporation
Research Triangle Park, NC 27709
EPA Contract No. 68-02-4392 j
EPA Project Officer: William B. Kuykendal
Office Of Air Quality Planning And Standards
Office Of Air And Radiation
U. S. Environmental Protection Agency
Research Triangle Park, NC 27711
May 1990
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This report has been reviewed by the Office Of Air Quality Planning And Standards, U. S. Environmental
Protection Agency, and has been approved for publication. Any mention of trade names or commercial
products is not intended to constitute endorsement or recommendation for use.
EPA-450/2-90-009
n
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REPORT USER FEEDBACK AND MAIL KEY REGISTRATION'
The U.S. Environmental Protection Agency's (EPA) Office of Air Quality
Planning and Standards (OAQPS) provides technical support to ass.ist State and
local air pollution control agencies in developing and implementing air toxics
programs. One way that OAQPS provides assistance to agencies and other
interested individuals is by compiling and publishing emission data for agencies
and others who are interested in locating potential emitters of toxic air
compounds and in making preliminary' estimates of toxic air emissions. These
reports published by EPA are introductory documents only, and they are not
intended to provide exact estimates of air toxics releases from specific
facilities. EPA will update and expand these reports and publish new documents
as toxic air emissions data are obtained. Your comments on the usefulness of
this report and availability of additional data which could be used to extend
and improve it, are important input to this process. Please provide any
information to us that will allow us to improve these reports. The format below
is provided for your convenience.
Please check the appropriate blanks and mail to:
Pollutant Characterization Section
Noncriteria Pollutant Programs Branch (MD-15)
U.S. Environmental Protection Agency
Research Triangle Park, North Carolina 557711
I have additional air toxics emission data that would help EPA. Please
contact me.
_.Other comments on the report or needs for similar reports. '
NAME:
POSITION:
COMPANY/AGENCY:
MAILING ADDRESS:
PHONE NUMBER: { )
REPORT TITLE:
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CONTENTS
Figures '
Tables ' ' * ' 1V
. v
1. Purpose of Document ! , ,
2. Overview of Document Contents. .. ..'*** i";
3. Background Information ' ' £"}
3.1 Characterization of the Industry ."'. " •••*••-.•••••. *-J.
3.2- Incinerator Process Descriptions ... 33
3.3 Emissions and Controls .... ^"fo
3.4 References *i ;"**
4. Emission Factors .......... \ *. ". " ' ^ ''
4.1 Emission Factors for Multiple Dearth Furnaces." ." ' ' " * Tl
4.2 Emission Factors for Fluidized Bed Combustors. ..'"'' 411
4.3 Emission Factors for Organic Compounds . . . ' " 4
4.4 Other Combustor Types 7 };
4.5 References ' i *"**
5. Sampling and Analysis Procedures ..'**' ' ' * * J"f
5.1 Particulate Determination by EPA Method's! .'!]'*' ' Sli
i*l rnl^Dete>™ination by EPA/EMSL Draft Protocol. . " ' ' 5-1
5.3 CDD^CDF and PCB/PAH/CB/CP Determination
by the Draft ASME/EPA Method .... 5 3
5.4 Volatile Organic Sampling Train (VOST) Method! 5.7
5.5 . Particle size Semivolatile Organic Determination ' ' ' '
c e on 5"e fource Assessment Sampling System (SASS). . . 5.17
5.6 Sludge Analyses . \ \'
5.7 References . • •••••- s-i/
Appendices
A. U.S. Sewage Sludge Incinerators
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iii
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FIGURES
Page
Number .
3-1 U.S. geographic distribution of sewage incineration . . .... 3-2
3-2 Cross section of a multiple hearth furnace. ..... 3.4
3-3 Cross section of a fluidized bed furnace 3.7
3-4 Cross section of an electric infrared furnace 3-10
3-5 Venturi/fmpingement tray scrubber ''..... 3-15
5-1 Participate sampling train 5_2
5-2 EMSL metals sampling train configuration. . ,. 5.4
5-3 Digestion and analysis scheme for EMSL trace metal
train components r front half 5-5
5-4 CDD/CDF/CB/CP/PCB/PAH sampling train configuration 5.3
5-5 Extraction and analysis schematic for CDD/CDfr/CB/CP/PCB/PAH
flue gas samples 5.9
VOST analysis protocol ...... 5-15
VOST sampling train configuration -....».. 5-15
SASS sample diagram 5_ls
5-9 SASS sample handling and transfer: nozzle, urobe
cyclones and filter ...........!...' 5_lg
i
5-10 SASS sample handling and transfer: organic module section. . . 5-20
5-11 SASS sample handling and transfer: impinger train 5-21
5-12 Analysis protocol for metals in sludge. ...!..' 5.22
5-13 Analysis protocol for volatile organics in solid wastes .... 5-23
5-6
5-7
5-8
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TABLES
Number
4-1 Inorganic Compound Emission Factors on a Compound Feed Basis
for Multiple Hearth Furnaces Burning Sewage Sludge . . . . . . .4.3
4-2 Inorganic Compound Emission Factors on a Total Particulate
Emission Basis for Multiple Hearth Furnaces Burning
Sewage Sludge.
4-5
4-3 Inorganic Compound Emission Factors in SI Units on a Total
Feed Basis for Multiple Hearth Furnaces Burning
Sewage Sludge . 7
4-4 Inorganic Compound Emission Factors.in English Units on a
Total Feed Basis for Multiple Hearth Furnaces Burning
Sewage Sludge. .
4-9
4-5 Inorganic Compound Emission Factors on a Compound Feed Basis
tor Fluidized Bed Combustors Burning Sewage Sludge 4-12
4-6 Inorganic Compound Emission Factors on a Total Particulate
Emission Basis for Fluidized Bed Combustors Burnina
Sewage Sludge • . . ' •
4-7 Inorganic Compound Emission Factors in SI Units on a Total '
Feed Basis for Fluidized Bed .Combustors Burning
Sewage Sludge.
4-8 Inorganic Compound Emission Factors in English Units on a
Total Feed Basis for Fluidized Bed Combustors Burning
N0W9rtO X"l iirlna «*
Sewage Sludge.
4-13
4-14
4-15
4-9 Volatile Organic Compound Emission Factors"in SI Units for
Incinerators Burning Sewage Sludge ; .......... 4-16
« '
4-10 Volatile Organic Compound Emission Factors in English Units
for Incinerators Burning Sewage Sludge ....... . . . . 4-17
4-11 Semivolatile Organic Compound Emission Factors in SI Units
for Incinerators Burning Sewage Sludge . . .! .... 4-18
4-12 Semivolatile 9rganic Compound Emission Factors in English
units for Incinerators Burning Sewage Sludge . . 4.19
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TABLES, Continued
Number , Pace
5-1 Typical CDD/CDF Target Cogeners . ' '. . . 5-11
5-2 Typical CB, PCB, CP, and PAH Target Compounds .... 5-12
5-3 Typical Target VOC 5-14
gap.001 vi
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1. PURPOSE OF DOCUMENT
. . !•» "
This document is designed to assist Federal, State, and local air
pollution agencies in inventorying air emissions of potentially toxic
substances. It is one of a series the Environmental Protection Agency (EPA)
is preparing to "compile information on sources and emissions of these
pollutants. Specifically, this document deals with emissions from sewage
sludge incinerators (SSIs). j
The emissions information in this document will be most useful in
making preliminary estimates of air emissions and should not be used in
exact assessments of emissions from any particular facility. The reason for
this is that insufficient data are available to estimate the statistical
accuracy of these emission factors. In addition, variability in sludge
composition contributes to variations in emission factors. In fact, the
difference between actual and calculated emissions could be as.great as
orders of magnitude in extreme cases. The size of error would depend on
differences in source configurations, variability of sludge composition,
control equipment design and operation, and overall operating practices. A
source test is the best way to determine a.ir emissions from a particular
source. However, even when a source test is used for a specific facility,
variability of sludge composition could change the composition of emissions.
To date, 22 reports in this series have been published, each with the
generic title "Locating and Estimating (Toxic) Emissions from (or of)
(Source Category or Substance)." Reports are available for the following
substances or source categories: acrylonitrile, 1,3-butadiene, carbon
tetrachloride, chloroform, ethylene dichloride, formaldehyde, nickel,
chromium, manganese, phosgene, epichlorohydrin, vinylidene chloride,
ethylene oxide, chlorobenzenes, polychlorinated biphenyls (PCBs), polycyclic
organic matter (POM), benzene, organic liquid storage tanks, coal and oil
combustion sources, municipal waste combustors, perchloroethylene and
trichloroethylene. A reports is in production for styrene and others are
planned..
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2. OVERVIEW OF DOCUMENT
* i »
i
!
This section briefly outlines the contents of this report.
Section 3 is an overview.of the sewage sludge incineration (SSI)
industry, describing the major types of SSIs in the existing population:
multiple hearth furnaces, fluidized bed furnaces, and electric furnaces!
Several types of lesser importance are also presented. Included is a
process description for each type of combustor, as well as a current
facility list. In addition, this section describes the air emission control
technologies currently in use at SSI facilities.
Section 4 focuses on the air emissions from SSIs. Emission factors are
given in tabular format for organics and inorganics including metals.
Section 5 discusses the EPA reference methods and generally accepted
methods of sampling and analysis for each pollutant. Appendix A contains a
list of the existing SSI facilities. Included in the list are incinerator
«
type, unit size, start-up date and type of air pollution control device.
This document does not discuss health or other environmental effects of
emission from SSIs, nor does it discuss ambient air levels or ambient air
monitoring techniques for emissions associated with SSIs.
Comments on this document are welcome, including information on process
descriptions, operating practices, control measures, and emissions
information that would enable EPA to improve the contents. All comments
should be sent to: . ! '
Chief, Pollutant Characterization Section (MD-15)
Noncriteria Pollutant Programs Branch
U. S. Environmental Protection Agency
Research Triangle Park, North Carolina 27711
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3. BACKGROUND INFORMATION . "
i
Incineration is a means of disposing of sewage sludge generated by the
treatment of wastewater from residential, commercial, and industrial
establishments. When compared to other forms of disposal, incineration has,
the advantages of reducing the solid mass and the potential for recovering
energy through combustion. Disadvantages include the necessity of ash
disposal and the 'potential for air emissions of pollutants.
This section provides background information on the current status of
sewage sludge incineration. In Section 3.1, the sewage sludge incineration
industry is briefly overviewed. Incinerator and emission control design are
described in detail in Sections 3.2 and 3.3, respectively.
3.1 CHARACTERIZATION OF THE INDUSTRY
There are currently about 200 sewage sludge incineration (SSI) plants
in operation in the United States. Three main types of incinerators are
used: multiple hearth, fluidized bed, and electric infrared. Some sludge
is co-fired with municipal solid waste in combustors based on refuse
combustion technology. Unprocessed refuse co-fired with sludge in
combustors based on sludge incinerating technology is limited to multiple
hearth incinerators only. . |
Over 80 percent of the identified operating sludge incinerators are of
the multiple hearth design. About 15 percent are fluidized "bed combustors
and 3 percent are electric. The remaining combustors co-fire refuse with
sludge.
Figure 3-1 shows the approximate geographic distribution of the
existing SSI population. Most sludge incineration facilities are located in
the Eastern United States, though there are a significant number on the West
Coast. New York has the largest number of facilities with 33. Pennsylvania
and Michigan have the next-largest numbers of facilities with 21 and
19 sites, respectively.
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3-2
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•
•
•
•
•
t
•
A list of the existing facilities is in Appendix A. Table A-1 is
sorted by combustor technology, and shows incinerator type, unit capacity,
year of facility start-up, and type of air pollution control device.
3.2 INCINERATOR PROCESS DESCRIPTIONS
Types of incineration described in this section include:
Multiple hearth
Fluidized bed
Electric
Single hearth cyclone
Rotary kiln
High pressure, wet air oxidation
Co-incineration with refuse
•
3.2.1 Multiple Hearth Furnaces
The multiple hearth furnace was originally developed for mineral ore
roasting nearly a century ago. The air-cooled variation has been used to
incinerate sewage sludge since the 1930's. A cross section diagram of a
typical multiple hearth furnace is shown in Figure 3-2. The basic multiple
hearth furnace (MHF) is cylinder-shaped and oriented vertically. The outer
shell is constructed, of steel, lined with refractory, and surrounds a series
of horizontal refractory hearths. A hollow cast iron rotating shaft runs
through the center of the hearths. Cooling air for the center shaft and
rabble arms is introduced into the shaft by a fan located at its base.
Attached to the central shaft are the rabble arms,;which extend above the
hearths. Each rabble arm is equipped with a number- of teeth, approximately
6 inches in length, and spaced about 10 inches apart. The teeth are shaped
to rake the sludge in a spiral motion, alternating in direction from the
outside in, to the inside out, between hearths. Typically, the upper and
lower hearths are fitted with 4 rabble arms, and the middle hearths are
fitted with two. Burners, providing auxiliary heat, are located in the
sidewalls of the hearths.
i
Partially dewatered sludge is fed onto the perimeter of the top hearth
by conveyors or pumps. The motion of the rabble arms rakes the sludge
toward the center shaft where it drops through holes located at the center
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COOLING AIR
DISCHARGE
SCUM
AUXILIARY/
AIR PORTS
RABBLE ARM
2 OR 4 PER
HEARTH
CLINKER
BREAKER
ASH
DISCHARGE
BURNERS
SUPPLEMENTAL
FUEL
COMBUSTION AIR
SHAFT COOLING
AIR RETURN
SOLIDS FLOW
DROP HOLES
Figure 3-2. Cross section of a multiple hearth furnace.
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of the hearth. In the next hearth the sludge is raked in the opposite
direction. This.process is repeated in all of the subsequent hearths. The
effect of the rabble motion is to break up solid material to allow better
surface contact with heat and oxygen, and is arranged so that sludge depth
of about one inch is maintained in each hearth at the design sludge flow
rate. . l . . •
r
Scum may also be fed to one or more hearths of the incinerator. Scum
is the material that floats on wastewater. It is generally composed of
vegetable and mineral oils, grease, hair, waxes, fats;, and other materials
that will float and usually has a higher heating value and larger volatile
fraction than sludge. Scum may be removed from many treatment units
including preparation tanks, skimming tanks, and sedimentation tanks.
Quantities of scum are generally small compared to those of other wastewater
solids.
Ambient air is first ducted through the central shaft and its
associated rabble arms. A portion, or all, of this air is then taken from
the top of the shaft and recirculated into the lowermost hearth as preheated
combustion air. Shaft cooling air which is not circulated back into the
furnace is ducted into the stack downstream of the air pollution control
devices. The combustion air flows upward through the drop holes in the
hearths, countercurrent to the flow of the sludge, before being exhausted
from the top hearth. Provisions are usually made to inject ambient air
directly into on the middle hearths as well.
From the standpoint of the overall incineration process, multiple •
hearth furnaces can be divided into three zones. -The upper hearths comprise
the drying zone where most of the moisture in the sludge is evaporated. The
temperature in the drying zone is typically between 425 and 760°C (800 and
1,400 F). Sludge combustion occurs in the middle hearths (second zone) as
the temperature is increased between 815 and B2S°t (1,500 and 1,700°F). The
combustion zone can be further subdivided into the upper-middle hearths
where the volatile gases and solids are burned, and the lower-middle hearths
where most of the fixed carbon is combusted. The third zone, made up of the
lowermost hearth(s), is the cooling zone. In this zone the ash is cooled as
its heat is transferred to the incoming combustion air.
gep.003 3.5
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Multiple hearth furnaces are sometimes operated with afterburners to
further reduce odors and concentrations of unburned hydrocarbons In
afterburning, furnace exhaust gases are ducted to a chamber where they are
mixed with supplemental fuel and air and completely combusted. Some
incinerators have the flexibility to allow sludge to be fed to a lower
hearth, thus allowing the upper hearth(s) to function essentially as an
afterburner. • ' - .
Under normal operating conditions, 50 to 100 percent excess air must be
added to an MHF in order to ensure complete combustion of the sludge
Besides enhancing contact between fuel and oxygen in the furnace, these
relatively high rates of excess air are necessary in order to compensate for
normal variations in both the organic characteristics of the sludge feed and
the rate at which it enters the incinerator. When an inadequate amount of
excess air is available, only partial oxidation of the carbon will occur
with, a resultant increase in emissions of carbon monoxide, soot, and
hydrocarbons. Too much excess air, on the other hand, can cause increased
entrapment of particulate and unnecessarily high auxiliary fuel
consumption.
Some MHFs have been designed to operate in a starved air mode. Starved
air combustion (SAC) is, in effect, incomplete combustion. The key to SAC
-is the usage of less than theoretical quantities of air in the
f'ueTemc^t t9H° PerC6nt °f St°iCh10metr1C <"»««•«• This makes SAC more
fuel efficient than an excess air mode MHF. The SAC reaction products are
combustible gases, tars and oils, and a solid char that can have appreciable
heating value. The most effective utilization of these products is by
burning of the total gas stream with subsequent heat recovery. When an
SAC MHF is combined with an afterburner, an overall excess air rate of 25 to
50 percent can be maintained (as compared to 75 to 200 percent overall for
an excess air MHF with an afterburner).
Multiple hearth furnace emissions are usually controlled by a venturi
scrubber, an impingement tray scrubber, or a combination of both Wet
cyclones are also used.
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SAND
FEED'
THERMOCOUPLE
FREEBOARD
SLUDGE.
INLET
SAND BED >:-:
Vrr 'T^-fr -ffin rffri
i ^^ II i r rr
.FLUIDIZ1NG
AIR INLET
REFRACTER
ARCH
^ EXHAUST AND ASH
WINDBOX
PRESSURE TAP
...SIGHT
Y GLASS
- TUYERES
FUEL
GUN
PRESSURE TAP
STARTUP
-J PRIHEAT
pBURNER
-I FOR HOT
WINDBOX
Figure 3-3. Cross section of a fluidized bed furnace.
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3.2.2 Fluidlzed Bed Incinerators
Fluidized bed technology was first developed by the petroleum industry
to be used for catalyst regeneration. Fluidized bed technology was first
used for municipal sludge incineration in 1962. Figure 3-3 shows the cross
section diagram of a fluidized bed furnace (FBF). Fluidized bed furnaces
are cylindrically shaped and oriented vertically. The outer shell is
constructed-of steel, and is lined with refractory. Tuyeres (nozzles
designed to deliver blasts of air) are located at the base of the furnace
within a refractory-lined grid. A bed of sand, approximately 0.75 meters
(2.5 feet) thick, rests upon the grid. Two general configurations can be
distinguished on the basis of how the fluidizing air is injected into the
furnace. In the "hot windbox" design the combustion air is first preheated
by passing through a heat exchanger where heat is recovered from the hot
flue gases. Alternatively, ambient air can be injected directly into the
furnace from a cold windbox.
Partially dewatered sludge is fed into the bed of the furnace. Air
injected through the tuyeres, at pressure of from 20 to 35 kPa (3 to
5 psig), simultaneously fluidizes the bed of hot sand and the incoming
sludge. Temperatures of 725 to 825°C (1,350 to 1,500°F) are maintained in
the bed. Residence times are on the order of 2 to 5 seconds. As the sludge
burns, fine ash particles are carried out the top of t'he furnace. Some sand
is also removed in the air stream; sand make-up requirements are on the'
order of 5 percent for every 300 hours of operation.
The overall process of combustion of the sludge occurs in two zones.
Within the bed itself (zone 1) evaporation of the water and pyrolysis of the'
organic materials occur nearly simultaneously as the temperature of the
sludge is rapidly raised.. In the second zone, (freeboard area) the
remaining free carbon and combustible gases are burned. The second zone
functions essentially as an afterburner.
Fluidization achieves nearly ideal mixing between the sludge and the
combustion air and the turbulence facilitates the transfer of heat from the
hot sand to the sludge. The most noticeable impact of the better burning
atmosphere provided by a fluidized bed incinerator is seen in the limited
amount of excess air required for complete combustion of the sludge.
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.
These incinerators cantachieve complete combustion with 20 to 50 percent
excess air, about half the amount of excess air typically required for
incinerating sewage sludge in multiple hearth furnaces. As a consequence,
FBF incinerators have generally lower fuel requirements compared to MHF '
incinerators. .
Fluidized bed incinerators most often have venturi, scrubbers, or
venturi/impingement tray scrubber combinations for emissions control.
3.2.3 Electric Incinerators
Electric furnace technology is new compared to other sludge combustor
designs; the first electric furnace was installed in 1975. Electric
incinerators consist of a horizontally oriented, insulated furnace. A woven
wire belt conveyor extends the length of the furnace and infrared heating
elements are located in the roof above the conveyor belt* Combustion air is
preheated by the flue gases and is injected into the discharge end of the
furnace. Electric incinerators consist of a number of prefabricated
modules, which can be linked together to provide the necessary furnace
length. A cross section of an electric furnace is shown in Figure 3-4.
The dewatered sludge cake is conveyed into one end of the incinerator.
An internal roller mechanism levels the sludge into; a continuous layer
approximately one inch thick across the width of the belt. The sludge is
sequentially dried and then burned as it moves bene;ath the infrared heating
elements. Ash is discharged into a hopper at the apposite end of the
furnace. The preheated combustion air enters the furnace above the ash
hopper and is further heated by the outgoing ash. The direction of air flow
is countercurrent to the movement of the sludge along the conveyor. Exhaust
gases leave the furnace at the feed end. Excess air rates vary from 20 to
70 percent.
When compared to MHF and FBF technologies, the electric furnace offers
the advantage of lower capital cost, especially for smaller systems.
However, electric costs in some areas may make an electric furnace
infeasible. Another concern is replacement of various components such as
the woven wire belt and infrared heaters, which have 3 to 5 year lifetimes.
Electric incinerators are usually controlled with a venturi scrubber or
some other wet scrubber. I
gep.003 3.9
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01
3-10
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3.2.4 Other Technologies
A number of other technologies have been used for incineration of
sewage sludge including cyclonic reactors, rotary kilns and wet oxidation
reactors. These processes are not in widespread use iin the United. States
and will be discussed only briefly.
The cyclonic reactor is designed for small capacity applications. It
is constructed of a vertical cylindrical chamber that is lined with
refractory. Preheated combustion air is introduced into the chamber
tangentially at high velocities. The sludge is sprayed radially toward the
hot refractory walls. Combustion is rapid: the residence time of the
sludge in the chamber is on the order of 10 seconds. The ash is removed
with the flue gases.
Rotary kilns are also generally used for small capacity applications.
The kiln is inclined slightly from the horizontal plane, with the upper end
receiving both the sludge feed and the combustion air. A burner is located
at the lower end of the kiln. The circumference of the kiln rotates at a
speed of about 6 inches per second. Ash is deposited into a hopper located
below the burner.
The wet oxidation process is not strictly one of incineration; it
instead utilizes oxidation with air at elevated -temperature and pressure in
the presence of water (flameless combustion). Thickened sludge, at about
six percent solids, is first ground and mixed, with a stoichiometric amount
Decompressed air. The sludge-air mixture is then preheated in a heat
exchanger using the reactor effluent stream as the Ifieat source before
entering the pressurized reactor. The temperature of the reactor .is held
between 175 and 315°C (350 and 600°F). The pressure is normally 7,000 to
12,500 kPa (1,000 to 1,800 psig). Steam is usually used for auxiliary
heat. The water and resulting ash are circulated out the reactor and are
separated in a tank or lagoon. The liquid phase is recycled to the
treatment plant. Off-gases must be treated to eliminate odors: wet
scrubbing, afterburning or carbon absorption may be used.
3.2.5 Co-incineration with Refuse
Wastewater treatment plant sludge generally has a high water content
and in some cases, fairly high levels of inert materials. As a result, its
gep.003 3.
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net fuel value is often low. 'if sludge is combined with other combustible
materials in a co-combustion scheme, a furnace feed can be created that has
both a low water concentration and a heat value high enough to sustain
combustion with little or no supplemental fuel.
Virtually any material that can be burned can be combined with sludge
in a co-combustion process. Common materials for co-combustion are coal,
municipal solid waste, wood waste and agricultural waste. Thus, a municipal
or industrial waste can be disposed of while providing an autogenous
(self-sustaining) sludge feed, thereby solving two disposal problems.
There are two basic approaches to combusting sludge with municipal
solid waste (MSW): 1) use of MSW combustion technology by adding dewatered
or dried sludge to the MSW combustion unit, and 2) use of sludge combustion
technology by adding raw or processed MSW as a supplemental fuel to the
sludge furnace.
With the latter, MSW is processed by removing noncombustibles,
shredding, air-classifying, and screening. Waste that is more finely
'processed is less likely to cause problems such as severe erosion of the
hearths, poor temperature control, and refractory failures.2
3.3 EMISSIONS AND CONTROLS
Sewage sludge incinerators potentially emit significant quantities of
pollutants. The major pollutants emitted are: 1) particulate matter,
2) metals, 3) carbon monoxide (CO),'4) nitrogen oxides (NOX), 5) sulfur
dioxide (S02) and 6) unburned hydrocarbons. Partial combustion of sludge
can result in emissions of intermediate products of incomplete combustion
(PICs) including toxic organic compounds. •
Uncontrolled particulate emission rates vary widely depending on the
type of incinerator, the volatiles and moisture content of the sludge, and
the operating practices employed. Generally, uncontrolled particulate
emissions are highest from fluidized bed incinerators because suspension
burning results in much of the ash being carried out of the incinerator with
the flue gas. Uncontrolled emissions from multiple hearth and fluidized bed
incinerators are extremely variable, however. Electric incinerators appear
to have the lowest rates of uncontrolled particulate release of the three
gep.003
3-12
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major furnace types, possibly because the sludge is not disturbed during *
firing. In general, higher airflow rates increase the opportunity for
particulate matter to be entrained in the exhaust gases. Sludge with low
volatile content or high moisture content may compound this situation by
requiring more supplemental fuel to burn. As more fuel is consumed, the
amount of air flowing through the incinerator is also increased. However,
no direct correlation has been established between air flow and particulate
emissions. I.
Metals emissions are affected by fuel bed temperature and the level of
particulate matter control, since metals which are volatilized in the
combustion zone condense in the exhaust gas stream. Most metals (except
mercury) are associated with fine particulate and are removed as the fine
particulates are removed.
Carbon monoxide is formed when available oxygen Is' insufficient for
complete combustion or when excess air levels are too high, resulting in
lower combustion temperatures.
Nitrogen and sulfur oxide emissions are primarily the result of
oxidation of nitrogen and sulfur in the sludge. Therefore, these emissions
can vary greatly based on local and seasonal sewage characteristics. '
Emissions of"volatile organic .compounds also vary greatly with
incinerator type and operation. Incinerators with countercurrent air flow
such as multiple hearth.designs provide the greatest opportunity for
unburned hydrocarbons to -be emitted. In the MHF, hot air and wet sludge
feed are contacted at the top -of the furnace. Any compounds distilled from
the solids are immediately vented from the furnace at temperatures too low
to completely destruct them.
Particulate emissions from sewage sludge incinerators have historically
been controlled by wet scrubbers, since the associated sewage treatment
plant provides both a convenient source and a good-disposal option for the
scrubber water. The types of existing sewage sludge incinerator controls
range from low pressure drop spray towers and wet cyclones to higher
pressure drop venturi scrubbers and venturi/impingement tray scrubber
combinations. A few electrostatic precipitators are employed, primarily
where sludge is co-fired with municipal solid waste and baghouses have been
gep.003 • 3_13
-------
used. The most widely used control device applied to a multiple hearth
incinerator is the impingement tray scrubber. Older units use the tray
scrubber alone while combination venturi/impingement tray scrubbers are.
widely applied to newer multiple hearth incinerators and to fluidized bed
incinerators. Most electric incinerators and some fluidized bed
incinerators use venturi scrubbers only.
In a typical combination venturi/impingement tray scrubber (shown 'in
Figure 3-5), hot gas exits the incinerator and enters the precooling or
quench section of the scrubber. Spray nozzles in the quench section cool
the incoming gas and the quenched gas then enters the venturi section of the
control device.
Venturi water is usually pumped into an inlet weir above the quencher.
The venturi water enters the scrubber above the throat and floods the throat
completely. This eliminates build-up of solids and reduces abrasion.
Turbulence created by high gas velocity in the converging throat section-
deflects some of the water traveling down the throat into the gas, stream.
Particulate matter carried along with the gas stream impacts on these water
particles and on the water wall. As the scrubber water and flue gas leave
the venturi section, they pass into a flooded elbow where the stream
velocity decreases, allowing the water and gas to separate. Most venturi
sections come equipped with variable throats. By restricting the throat
area within the venturi, the linear gas velocity is increased and the
pressure drop is subsequently increased. Up to a certain point, increasing
the venturi pressure drop increases the removal efficiency. Venturi
scrubbers typically attain 60 to 99 percent removal efficiency for
^articulate matter, depending on pressure drop and particle size
distribution.3
At the base of the flooded elbow, the gas stream passes through a
connecting duct to the base of the impingement tray tower. Gas velocity is
further reduced upon entry to the tower as the gas stream passes upward
through the perforated impingement trays. Water usually enters the trays from
inlet ports on opposite sides and flows across the tray. As gas passes
through each perforation in the tray, it creates a jet which bubbles up the
water and further entrains solid particles. At the top of the tower is a
gep.003
3-14
-------
QM Exit to Induced Draft
Fan and Stack
Water
Weir
Box-
Quencher-
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Exhaust
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Figure 3-5. Venturi/impingement tray scrubber.
gep.003
3-15
-------
mist eliminator to reduce the carryover of water droplets In the stack
effluent gas. The Impingement section can contain from one to four trays,
but most systems for which data are available have two or three trays.
gep.003
3-16
-------
3.4 REFERENCES
i
1. Second Review of Standards of Performance for Sewage Sludge
Incinerators. EPA-450/3-84-010, U.S. Environmental Protection Agency,
Research Triangle Park, NC. March 1984.
i .
2. Process Design Manual for Sludge Treatment and Disposal.
EPA-625/1-79-011, U.S. Environmental Protection Agency, Cincinnati, OH.
September 1979.
3. Control Techniques for Particulate.Emissions From Stationary Sources -
Volume 1. EPA-450/3-81-005a, U.S. Environmental Protection Agency,
Research Triangle Park, NC. September 1982.
gep.003
3-17
-------
-------
4. EMISSION FACTORS
* I •
• . «• I
Emission factors have been developed for the various pollutants emitted
from SSIs. These emission factors are derived from published emissions
data; no new sampling of sources was done for this; project. The factors
relate the amount of pollutant emitted in the flue gas to the amount of
sludge incinerated and may be used to estimate emissions from a facility.
Flue gas emissions are the principal source of air toxics emissions from
sewage sludge incinerators. The estimated emissions should be used with
caution, however, because the emission factors are generally averages from
several facilities and are not necessarily representative of the emissions
from any particular facility. Additionally, because of limited data, a
representative number of facilities could not be used in evaluating emission
factors. In some cases, data from only one facility were available; these
factors are noted individually, and should only be used with extreme
caution. . ,
If more accurate emission estimates are needed, source testing should
be done. Data collected should include sludge feed rate and composition,
ash composition, and stack emissions. The actual air toxics emissions from
*•
any given facility are a function of variables such as capacity, throughput,
1 ' i
sludge composition, operating characteristics, and air pollution control
device operations. The effects of these factors should be considered when
testing. If such testing is done, the Pollutant Characterization Section
requests copies of the tests be submitted so that better databases and
emission factors may be developed in the future.
In this document, emission factors are presented for 32 inorganic
compounds including metals,' 25 volatile organic compounds,- various isomers
of chlorinated dibenzo-p-dioxins and dibenzofurans; (CDD and CDF), and
7 other semivolatile organic compounds. Average emissions factors were
evaluated per incinerator type and emission control type. The overall
averages were derived by combining the average emission factors for each
test of the same general incinerator and emission control type. For
gep.003 4-1
-------
facilities where multiple operating conditions were evaluated or multiple
tests were performed over a period of years, the average emission factor
from each test condition or test was used in deriving the overall average.
Several individual emission factors were derived for each facility.
For inorganic compounds, three factors were derived by dividing the mass
emission rate of the pollutant.by 1) the measured feed rate of that
pollutant, by 2) the total particulate matter emission rate, and by 3} the
total dry sludge feed rate. Which factor is selected to estimate emissions
will depend on what information is available.. The first factor should be
used when the sludge feed composition is known in addition to the total dry
sludge feed rate. The second factor can be used to predict emissions of
specific compounds from the total particulate matter emission rate. The
third factor can be used if only the total sludge feed rate is known.
Organic compound emission factors were derived by dividing the mass emission
rate of the pollutant by the total dry sludge feed rate.
The first two inorganic compound factors are presented on a fractional
mass basis (ppm). All the emission factors o.n a total feed basis are
presented in both SI and English units. When a pollutant was. not detected,
no value was reported; overall average emission factors include data from
only those facilities where the compound was detected.
Emission factors for the different types df combustors and emission
controls are presented in Sections 4.1 to 4.3.
4.1 EMISSION FACTORS FOR MULTIPLE HEARTH FURNACES
Emission factors for inorganic compound emissions from multiple hearth
furnaces are presented in Tables 4-1 through 4-4. The emission factors are
for uncontrolled flue gas emissions as well as controlled flue gas
emissions. Emission factors for controlled emissions are separated by the
different types of-emission controls used with multiple hearth furnaces
including cyclones, impingement tray scrubbers, venturi scrubbers and
exhaust gas afterburners. Test data from facilities using a venturi
scrubber (with or without other devices) are reported separately from those
facilities using only low-energy scrub'bers. In addition, pilot scale test
data are presented for control by an electrostatic precipitator and by a
gep.003
4-2
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4-8
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TABLE 4-4. INORGANIC COMPOUND EMISSION FACTORS IN ENGLISH UNITS ON A TOTAL FEED BASIS
FOR MULTIPLE HEARTH FURNACES BURNING SEUAGE SLUDGE
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fabric filter. It shouVd be noted that data from reference 14 are
apparently biased high. The test report authors noted, but did not explain
their "consistent error", and reported an average of 20 percent more mass
emitted than fed, on a compound-specific basis. No attempt has 'been made
here to adjust or modify the values reported by the original reference.
Unreasonable (physically impossible) results have been individually noted in
the tables. •
4.2 EMISSION FACTORS FOR FLUIDIZED BED COMBUSTORS
Emission factors for inorganic compound emissions from fluidized bed
combustors are presented in Table 4-5 through 4-8. Fluidized bed combustors
are generally controlled by high-energy scrubbers, and no data are available
for any other control devices. Emission factors are presented for both
uncontrolled and controlled emissions. i
4.3 EMISSION FACTORS FOR ORGANIC COMPOUNDS
Emission factors for volatile organic compounds are presented in
Tables 4-9 and 4-10 in SI and English units, respectively. All data are
from multiple hearth furnaces and are separated by control device type. All
tested facilities are controlled by a venturi scrubber; emissions controlled
by a scrubber and an afterburner are reported separately. Uncontrolled
emissions are also reported.
Emission factors for semivolatile compounds are reported in Tables 4-11
and 4-12 in SI and English units, respectively. .Emission .factors are for
uncontrolled and controlled emissions. All data are for emissions from
multiple hearth furnaces except one FBC data set controlled by a high energy
scrubber. The emission factors from the FBC facility were within the range
of the MHF data and were therefore not reported separately.
4.4 OTHER COMBUSTOR TYPES
Emission factors for the other sludge incinerator types described in
Section 3 have not been separately prepared because! of insufficient data.
The expected emissions from electric furnaces, single hearth cyclones,
rotary kilns, and high pressure wet air oxidation systems cannot be
quantified with the available data. Data for emissions from co-incineration
of sewage sludge with refuse are also not available.
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8.
4.5 REFERENCES
1. Knisley, D.R et al. (Radian Corporation). Site 1 Revised Draft
Emission Test Report, Sewage Sludge Test Program. Prepared for
U.S. Environmental Protection Agency, Water Engineering Research
Laboratory. Cincinnati, Ohio. February 9, 1989. pp. 4-n, 14, 15,
i
2- Knisley, D.R., et al. (Radian Corporation). Site 2 Final Emission Test
Prepared for U.S. Environmental Protection Agency™ Wate? Engineering"
Research I ahnratnvM/. Cincinnati Ohio n~ --— »•"==<_ i»y
'37, 70, 78, 79.
Test Results. Prepared for U.S. Environmental Protection Agency Water
Engineenng.Research^ Laboratory. Cincinnati, i Ohio. Octobe? TJislj
Knisley, O.R., et al. (Radian Corporation). Site 4 Final Emission Test
SeWTeStp Pr°9ram- ^"d'for U.S. Envi?onmen?al
o ter En9inee^ing Research Laijoratory. Cincinnati
PP> 4"16' 25' 26' 3°' 31" 6I' 67> 73, 86, 88 96,'
ExhatnfM SorP°ration)- Or^^ Emissions from the
txnaust Stack .of a Multiple Hearth Furnace Burning Sewaqe Sludae
Rp^a"6H fT U'?' Envi!:onmental Protection Agency? wKS EnglnSrlng
Researc^ Laboratory. Cincinnati, Ohio, September 30, 1985 pp.2?2,
Fvtnf aii (?adian Corporation). Partitulate Removal
Evaluation of an Electrostatic Precipitator Dust Removal System
rloa'rld^ u ^Ulrip^ Hea^h I^ine'rator Burning Sewage Sudge.
Sl«r h f r ?' Environmental Protection Agency, Water Engineering
Research5Laboratory.^Cincinnati, Ohio. September 30, 19859 pp 2?
a1-(Rad1an Corporation). Particulate Removal
C1nc1nnat1 •
•
Radian Corporation. Rhode Island Toxics Integration Project Phase TT-
Pr±,°H f1" |ffsi°2s from Two Sewa9e Sludge Inc neraHon Facilittes
MaS«S«nf°r otat^°f Rho^ Island Department of Environmental
Management. Providence, Rhode Island. June 30, 1988. p. 3-2.
gep.003
4-20
-------
9. Mclnnes, R.G., et a!., (GCA Corporation/Technology Division). Sampling
and Analysis Program at the New Bedford Municipal Sewage Sludge
Incinerator. Prepared for U.S. Environmental Protection Agency.
Research Triangle Park, North Carolina. November 1984. p. 5.
10. Hunt, 6., et al. Noncriteria Emissions Monitoring Program for the
Envirotech Nine-Hearth Sewage Sludge Incinerator at the Metropolitan
'Wastewater Treatment Facility. Prepared for Metropolitan Waste Control
Commission. St. Paul, Minnesota. October 1986. pp. 2-3, 5, 6, 7, 10,
11, 12, 14. . . '
11. Environment Canada. Organic and Inorganic Emissions from a Fluid Bed
Sewage sludge Incinerator at Duffin Creek Water Pollution Control
Plant. August 1988. pp. 31, 32.
12. Environment Canada. Organic and Inorganic Emissions from a
Multi-Hearth Sewage Sludge Incinerator at Highland Creek Water*
Pollution Control Plant. August 1988. p. 5.
13. Bridle,, T.R. (Environment (Canada). Assessment of Organic Emissions
from the Hamilton Sewage Sludge Incinerator, p.,3.
14. Farrell, J.B., et al. (U.S. Environmental Protection Agency). Air
Pollution Discharges from Ten Sewage Sludge Incinerators.
February 1981. pp. A-l, A-4> A-7 through A-22.
15. Keller, I.E., et al. (Radian Corporation). National Dioxin Study
Tier, 4- - Combustion Sources, "Final Test Report - Site 1 Sewage Sludge
Incinerator SSI-A. Prepared for U.S. Environmental Protection Agency.
April 1987. p. 5-27.
16. Palazzolo, M.A., et al. (Radian Corporation). National Dioxin Study
Tier 4 - Combustion Sources, Final Test Report - Site 3 Sewage Sludge
Incinerator SSI-B. Prepared for U.S. Environmental Protection Agency.
April 1987. p. 5-23.
17. Palazzolo, M.A., et al. (Radian Corporation). National Dioxin Study
Tier 4 - Combustion Sources, Final Test Report - Site 12 Sewage Sludge
Incinerator SSI-C. Prepared for U.S. Environmental Protection Agency.
April 1987. pp. 5-19, 5-27.
18. Dew!ing, R.T., R.M. Manganelli and G.T. Baer. Fate and Behavior of
Selected Heavy Metals in Incinerated Sludge. Journal of the Water
Pollution Control-Federation. Vol. 52, No. 10, October 1980.
pp. 2554, 2555. •
gep.003 4-21
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19. Bennet, R.L. .K-.T. JCnapp and D.L. Duke. Chemical and Physical
, of Municipal Sludge Incinerator Emissions; Report
-047. NTIS No. PB 84-169325. U..S. Environmental
Agency, Environmental Sciences Research Laboratory.
5?Sea£C5* "91e Park' North Carolina. March 1984. pp. 3, 24 26
20.
21
XI?!' ."^l!*?1 •"? oary Bel^zo- (GCA CorP') Performance of Emission
Tests and Material Balance for a Fluidized Bed Incinerator Final
Report. Prepared for U.S. Environmental Protection Agency, Division of
Stationary Source Environment, Washington, D.C. Contract U1*on
No. 68-01-4143. November 1980. pp. 20, 28, 29.
oln' Jny.7?nmfntal Protection Agency. Chromium Screening Study Test
Report (Vol. 1). Orgamcs Screening Study Test Report (Vol. 2)
Sewage Sludge Incinerator No. 13, Detroit Water and Sewer Dept.,
EHB Report
gap.003
4-22
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5. SAMPLING AND ANALYSIS PROCEDURES
The purpose of this section is to provide a brief discussion of the EPA
reference methods and/or generally accepted methods of sampling and analysis
used to gather emissions data on air toxics emitted from sewage sludge
incinerators. Different sampling and analytical methods than the ones
described may have been used previously. Slight modifications of the
methods may be specified by some State agencies to make results consistent
with their regulatory compliance results. However, these sampling methods
are widely used and accepted and should yield results comparable with data
from other facilities.
This section presents a general description of the sampling and
analytical methods for the determination of particuUte, metals, CDD/CDF and
other semiv.olatile organics, volatile organics and particle size air
emissions from sewage sludge incinerators. EPA reference methods are
described when available. Otherwise, the state-of-the-art draft methods are
described.
5.1 PARTICIPATE DETERMINATION BY EPA METHOD 5
The particulate mass is defined as any material iwhich condenses at or
above the filtration temperature of 248 ± 25°F after removal of uncombined
water. The Method 5 sampling train is shown in Figure 5-1,. The particulate
matter is withdrawn isokinetically and collected on the glass fiber filter.
The particulate sample is recovered by rinsing the glass probe liner
and front half of the glass filter holder with acetone. The acetone rinses
are evaporated and desiccated along with the filter.
weighed to a constant weight.
blank.1
Both fractions are
The final weight is adjusted for an acetone
5.2 METALS DETERMINATION BY EPA/EMSL DRAFT PROTOCOL
Sampling for particulate matter and toxic metals
according to the EPA draft protocol entitled "Methodology for the
Determination of Trace Metal Emissions in Exhaust Gases from Stationary
is currently performed
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5-2
-------
Source Combustion Processes."2 This method is applicable for the
determination of particulates and Pb, Zn P, Cr, Cu, Ni, Mn, Cd, Se, As, Hg,
Be, Th, Ag, Sb, and Ba emissions from, municipal waste incinerators, sewage
sludge incinerators, and hazardous waste incinerators. The metals sampling
train is shown in Figure 5-2.
Earlier sampling 'efforts may have employed EPA Method 12 which is
specifically designed for lead. With Method 12, the flue gas passed through
nitric acid only impingers which were than analyzed for the desired metals
in additional to lead. However, some metals such as nickel and mercury,
where found to be insufficiently collected in some cases.
The EPA draft method is based on Method 5 except for the following:
• The glassware is cleaned prior to sampling with an 8 hour soak in
10 percent (v/v) nitric acid solution.
• The impingers contain: i
first impinger - empty
second impinger - HN07/H,09
third impinger - HNCL/hLO/ i
fourth impinger - acTdic KMn04
The sampling train is recovered and the samples are analyzed according
to the scheme shown in Figure 5-3. The first, second and third impingers
are analyzed for all metals. The fourth impinger is analyzed only for
mercury which is typically not collected efficiently in the HN03/H202
impingers.
The digested samples are analyzed by inductively coupled argon plasma
(ICAP) spectroscopy for all metals except mercury. If arsenic or lead
levels are less than 2 ppm, graphite furnace atomic absorption spectroscopy
(AAS) is used. For mercury analysis, cold vapor AAS is used.
5.3 CDD/CDF AND PCB/PAH/CB/CP DETERMINATION BY THE DRAFT ASME/EPA METHOD
The state-of-the-art development for organics sampling is to collect
CDD/CDF, polychlorinated biphenyls (PCB), polynuclear aromatic hydrocarbons
(PAH), chlorobenzenes (CB), and chlorophenols (CP) in a single sampling
train and to separate the fractions during analysis.3!'4 Previous sampling
methods collected the CDD/CDF and PCB, PAH, CB and CP in separate trains
gep.003 5.3
-------
Isokinetic Sampling Heated Zone
^
• Filter
Glass Probe
^
r
i.
-*•
*
Impingers with
Absorbing Solutions
Ice Bath —
Empty'
HNOS HNO,
(All.
Metals)
(All
Metals)
\
Acidic
KMnO4
(Hg)
.Silica
Gel
Figure 5-2. EMSL metals sampling train configuration.
IT
to
5-4
-------
Front Half Sample Recovery Fraction*
Container No. 1
Fitter
Nozzle
Brush/Rinse
Probe, Cyteona Brush/Rinse
Dessicate;
Weigh
No. 3 Acetone
Discard
Evaporate;
De**icata; Weigh
Evaporate;
Dessicate: Weigh
Dissolve Residue
in HNO, Rinse
Divide into Two
Sections
Acidify to pH
with Nitric Acid
Reduce Volume
to ~50ml
by Heating
Digest each Section
with HF and HNO,
Using PRV's in the
Microwave or Parr
Bomb in a
Conventional Oven
Digest with HF and
HNO, using the
Microwave or Parr
Bomb in Conventional
Oven
(Fraction 1)
Futvr mo
Probe Rinse
Fraction 18
Filter and
Dilute to Volume
Fraction 1A
Analyze for Cd,
Cr.Ba, Be, Cu. Ni,
Ag, and Zn by (CAP
Add KM,O., Digest
with Acid and Potassium Persuifate
at 95° C in a Water Bath
or Convection Oven for 2 hrs.
Add Hydroxylamine,
Hydrochloride, and
Stannous Chloride
Analyze for Pb
Sb, Se. As by
AAS
C
Analyze for Hg
using Cold Vapor
AAS
Figure 5-3. Digestion and analysis scheme for EMSL 'trace metal train
components - front half.
a
ta
to
o
5-5
-------
U889L801
Contoinef No. 6
Impinger 5
(Silica Gel)
1 Weigh and
Oiscafd
I
\*
< >.*=
c u
re
C •(->
o c:
•»- tu
*J C
to O
DO.
cn S
v- O
Q U
tn
£'
5-6
-------
that were essentially identical.' Since December 1984 when the draft
ASME/EPA method was prepared, many modifications have been incorporated, not
all of which can be discussed in this brief section.
| _ 4*
The sampling train is based on Method 5, but as shown in Figure 5-4,
includes a condenser and XAD resin trap after the filter and before the
impingers. The sampling train glassware, XAD resin, and filters are cleaned
by baking, and rinsing with acetone and toluene prior to sampling. After
sampling, the sampling train is recovered with acetone followed by methylene
chloride and toluene rinses. The solvents should be of the highest grade"
available to prevent the introduction of chemical impurities which can
interfere with the quantitative analytical determinations.
The state-of-the-art extraction scheme is shown in Figure 5-5. The
extracted samples are analyzed by gas chromatography and mass spectroscopy
(GC/MS). The typical organics available are summarized in Tables 5-1
and 5-2. j
5.4 VOLATILE ORGANIC SAMPLING TRAIN (VOST) METHOD I
Sampling for volatile organic compounds (VOC) is conducted according to
SW-846, Method 0030. The sorbent cartridges are-analyzed according to
SW-846, Method 5040. Specific compounds of interest, which typically vary
depending on the test program, are listed in Table 5-3. A brief flow
diagram of the VOST,analysis is shown in Figure 5-6.!5
The VOST is designed to collect volatile organic compounds with boiling
points between 30°C and 100°C and has a flue gas detection limit of about
0.1 ug/m for most compounds. A schematic diagram of the VOST is shown in
Figure 5-7. The flue gas is sampled from the stack through a glass probe
with a glass wool plug. The probe temperature is maintained above 300°F.
The gas sample is then cooled to 68°F by a water-cooled condenser and passes
through a pair of resin traps in series, a silica gel drying tube, a
rotameter, a sampling pump, and a dry gas meter. The first resin trap
contains Tenax and the second trap contains Tenax followed by
petroleum-based charcoal. i
A VOST run consists of collecting four pairs of;traps, with each pair
used for 20 minutes at a sample flow rate of 1 liter per minute. The
gep.003 5-7
-------
JE
Zj
E
fO
i.
o
o
fr
fO
CQ
O
a.
§
I
in
5-8
-------
lortif leaglon Standard I
oltcobaoxaaa-dS (30 u«}
2-fluarophaoal (100 u«)
phanol-dS (100 u«>
2-iluorobtphaarL (30 u«)
t«rph.nrl-c«nd«rd
ZS • Intacnal icuuUcd
AS « Alcacnaea icwUcd
SX « Suzrofaca acandard
Extraction and analysis schematic for CDD/CDF/CB/CP/PCB/PAH
flue gas samples.
5-9
-------
CMKMU*
«x
•CMH/lbCl IUM.
MltltlM It *1
mo/or AI
wciM vich
lte* eJU«rt4
pi MJiuc
mp«tuoc u
liu rMn 3 •L
AM Kl U u 3
lit XAO Xuia Tr»
u
Sin*.. e{
Coll «a4 Zn4
half mt fUt.
I ua
IS t« Sexfaivc
l« Mtk nluaai
Figure 5-5. (Continued)
(SO
Z-flu*captuo«l (100
(100 04)
2-fluarablpbanrl (30 u«)
c«rph«nTl-iln (jo u«)
J.t.J',3' utz* «l-ei3 (
uphth*lhrn.l.n.-tlo (»
rh«nmrhr.M-4io (to
(40 u«)
(40 u«)
Cu-t.2.J.»,«.7.«.IpCBO
13c
"!'
01 -2.3,7,1-TCBO
3
eu-1.2.3,4,7,l-OCSO
C -1.2.3,7.1.»-!
1 C-1.2.3.»-TeBO
5-10
-------
TABLE 5-1. TYPICAL CDD/CDF TARGET CONGENERS
DIOXINS
i
Total trichlorinated dibenzo-p-dioxins (TrCDD)
2,3,7,8 tetrachlorodibenzo-p-dioxin (2,3,7,8 TCDD)
Total tetrachlorinated dibenzo-p-dioxins (TCDD)
1,2,3,7,8 pentachlorodibenzo-p-dioxin (1,2,3,7,8 PeCDD)
Total pentachlorinated dibenzo-p-dioxins (PeCDD)
1,2,3,4,7,8 hexachlorodibenzo-p-dioxin (1,2,3,4,7,8 HxCDD)
1,2,3,6,7,8 hexachlorodibenzo-p-dioxin (1,2,3,6,7,8 HxCDD)
1,2,3,7,8,9 hexachlorodibenzo-p-dioxin (1,2,3,7,8,9 HxCDD)
Total hexachlorinated dibenzo-p-dioxins (HxCDD)
1,2,3,4,6,7,8 heptachlorodibenzo-p-dioxin (1,2,3,4,6,7,8 HpCDD)
Total heptachlorinated dibenzo-p-dioxins (HpCDD)
Total octachlorinated dibenzo-p-dioxins (OCDD)
FURANS
Total trichlorinated dibenzofurans (TrCDF) |
2,3,7,8 tetrachlorodibenzofurans (2,3,7,8 TCDF)
Total tetrachlorinated dibenzofurans (TCDF) •
1,2,3,7,8 pentachlorodibenzofuran (1,2,3,7,8 PeCDF)
2,3,4,7,8 pentachlorodibenzofuran (2,3,4,7,8 PeCDF)
Total pentachlorinated dibenzofurans (PeCDF)
-1,2,3,4,7,8 hexachlorodibenzofuran (1,2,3,4,7,8 HxCDF)
1,2,3,6,7,8 hexachlorodibenzofuran (1,2,3,6,7,8 HxCDF)
2,3,4,6,7,8 hexachlorodibenzofuran (2,3,4,6,7,8 HxCDF)
1,2,3,7,8,9 hexachlorodibenzofuran (1,2,3,7,8,9 HxCDF)
Total hexachlorinated dibenzofurans (HxCDF) . j
1,2,3,4,6,7,8 heptachlorodibenzofuran (1,2,3",4,6,7,8 HpCDF)
1,2,3,4,7,8,9 heptachlorodibenzofuran (1,2,3,4,7,8,9 HpCDF)
Total heptachlorinated dibenzofurans (HpCDF)
Total octachlorinated dibenzofurans (OCDF)
gep.003 5-11
-------
TABLE 5-2. TYPICAL CB, PCB, CP, AND PAH TARGET COMPOUNDS
Chiorobenzenes
Total Dichlorobenzenes
1,2-dichlorobenzene
1,3-dichlorobenzene
1,4-di chlorobenzene
Total Trichlorobenzenes
1,2,4-tri chlorobenzene
1,3,5-tri chlorobenzene
1,2,3-trichlorobenzene
Polvchlorinated Biohenvls
Total Honochlorobiphenyls
2-chlorobiphenyl
Total Dichlorobiphenyls
2,3-dichlorobiphenyl
Total Trichlorobiphenyls
2,4,5-trichlorobiphenyl
*
Total Tetrachlorofaiphenyls
2,2'4,6-tetrachlorobiphenyl
Total Pentachlorobiphenyls
2,2/,3/,4,5-pentachlorobiphenyl
Chlorophenols
2-chlorophenoT
3-chlorophenol
4-chlorophenol
Total Dichlorophenols
2,3-dichlorophenol
2,4-di chlorophenol
2,5-dichlorophenol
2,6-dichlorophenol
3,4-dichlorophenol
3,5-dichlorophenol
Total Tetrachlorobenzenes
1,2,3,4-tetrachlorobenzene
1,2,3,5-tetrachlorobenzene
1,2,4,5-tetrachlorobenzene
Pentachlorobenzene
Hexachlorobenzene
Total Hexachlorobiphenyls
2,2'4,4,5,6'-hexachlorobiphenyl
Total Heptachlorobiphenyls
2,2'3,4,5',6,6-heptachlorobiphenyl
Total Octachlorobiphenyls
2,2',3,3,',4,5/,6,6'-octachloro-
biphenyl
Total nonachlorobiphenyls
. 2,2',353/,4,4',5,6,6'-nonachloro-
biphenyl
Decachlorobiphenyl
Total Tri chlorophenols
2,3,4-trichlorophenols
2,3,5-trichlorophenol
2,3,6-trichlorophenol
2,4,5-trichlorophenol
. 2,4,6-trichlorophenol
Total Tetrachlorophenols
2,3,4,6-tetrachlorophenol
2,3,5,6-tetrachlorophenol
(continued)
gep.003
5-12
-------
TABLE 5-2. (Continued)
Chlorophenols. (continued) , .
Pentachloropheriol
. 4-chloro-3-met,hyTphenol
Polvnuclear Aromatic Hydrocarbons i
1,4-Dichlorobenzene-d4
Naphtha!ene-d8
Acenaphthene-dlO
Acenaphthylene
Acenaphthene
FT uorene
Phenanthrene-dlO
Phenanthrene
Anthracene
Fluoranthene
Chrysene-dl2
Pyrene
Benzo(a)anthracene
Chrysene
Perylene-dl2
Benzo(b)fluoranthene
Benzo(k)f1uoranthene
Benzq(a)pyrene
Indeno(l,2,3-cd)pyrene
Dibenz(a;h)anthracene
Benzo(g,h,i)peryleqe
Benzo(e)pyrene
Perylene
gep.003 5-13
-------
TABLE 5-3. TYPICAL TARGET VOC
Acetaldehyde
Acrolein
•
•Acrylonitrile
Benzene
Bromodichloromethane
Carbon Tetrachloride
Chlorobenzene
Chloroethane
2-Chloroethylvinyl ether
Chloroform
Chloromethane
2-Chlorophenola
3-Chlorophenola
4-Chlorophenola
Chloropropane
2-Chloropropane
Dibromochloromethane •
1,1-Dichloroethane
1,2-Dichloroethane
4,2-Dichloroettiane
1,1-Dichloroethene
trans-l,2-D1chloroethene
1,1-Dichloroethylene .
Dichlprofluoromethane
1,2-Dichloropropane
cis-l,3-Dichloropropene
trans-1,3-Di chloropropene
Epoxyethane (ethylene oxide)
1,2-Epoxypropane (propylene oxide)
Ethyl benzene
Methylene Chloride
2-Nitropropane
PAN (Peroxyacetylnitrate)
Tetrach'I broetherie
Toluene
1,1,1-Trichloroethane
1,-1,2-Tri chl oroethane
Trichlorbethene
Trichlorofluoromethane
1,1,,2-Tri chloropropane
Vinyl Chloride
Measured in chlorophenol analysis.
gep.003
5-14
-------
VOST ANALYSIS PROTOCOL
Tenax and/or
Tenax-Charcoal Tube
Spike the Tube(s) with
100 ng dg Benzene while
at Room Temperature
Additional Spikes
d. Dlchloroethane
100 ng
P a rab romo fluoro-
benzene 200 ng
Place Tube(s) In Oesorptlon
Unit and Desorb for
10 Minutes at 180°C onto
the Analytical Trap
Use the Purge and Trap Apparatus
as Described 1n'Method 624
Rapidly Heat the Analytical Trap
to 180°C 4-5 minutes
Analyze the Desorbed Compounds
by GC/MS per Method 624
Figure 5-6. VOST analysis protocol.
gep.003
5-15
-------
OS
en
i*I
O
rtJ
en
a.
E
05
OO
O
f I iflMi
** ,= 3 5; g 4 2
i
in
-------
samples are collected at a fixed point representing average gas velocity.
Since the target species are gaseous components of the flue gas, isokinetic
sampling is not a consideration for this method.
5.5 PARTICLE SIZE SEMIVOLATILE ORGANIC SOURCE
ASSESSMENT SAMPLING SYSTEM (SASS)
Particulate matter and semivolatile organics are withdrawn at a constant
rate near isokinetic conditions. Three heated stainless steel cyclones
(10 urn, 3 urn and 1 urn) and a final filter collect and separate the
particulate matter. Since isokinetic sampling conditions are not
guaranteed, this method is not used for compliance determinations.
A schematic of the sampling train is shown in Figure 5-8. After the
cyclones and filter, the flue gas is cooled and organics are removed by a
sorbent cartridge. Following the sorbent cartridge is a set of impingers
which contain a nitric acid and peroxide mixture to condense moisture and
remove metals. The analytical scheme for the train is presented in
Figures 5-9, 5-10 and 5-11.6
5.6 SLUDGE ANALYSES
I
Sludge samples are often analyzed for metals, moisture and volatile
organics. The metals analyses are done according to SW-846, Method 3050 for
•digestion and Methods 6010, 7421 and 7060 for analysis. The analysis
protocol is shown in Figure 5-12. -. j
The volatile organic analysis follows SW-846, Method 8240. The
analysis protocol is shown in Figure 5-13.
gep.003 5-17
-------
ISOLATION
BALL VALVE
CASCOOUI
IMF/COOLER
TRACE ElEUCMT
COLLECTOR
PtYGAS WfTtH/OIIFtCE METQ
C£NTKAIIZEO TEMKRATURE
_ANO MESSUtE IEAOOUT
CONTtOL MOOUU
TWO I»HJAHM VACUUM fUMTS
Figure S-3. SASS sample diagram.
Source: IERL Procedures Manual: Level 1
Environmental Assessment Second Edition, EPA-600/7-78-201
gep.003
5-18
-------
NOZZLE
ANO
OM ftlNSI
IMUSM UNTIL MINIS
AMfAMS CLIAN
AOO SMUSH niNSt
10 -i
i CYCLONf
TAP ANO IMUSH CONTINTS
»BOM WAULS INTO LOWIR CU»
HIMOVf CUV ANO THANWIH
CONTINTS TO HOLF CONTAIN!*
KtCONNf CT CUV: MINSf CT-
CLONt WALLS ANO INT(K.
eoNNtcriNa TUIING INTO
LOWiH CU* WITH CM,CI,.CM-OH
HIMOVi I.OWfn CUF ANO THA
fin COMTINTS USINO CH.CL,:
CMjOM * Z
J - . CTCLOMf
1AMI AS 10 - «m CVCLON*
1 ->«
CYCLONf
SAMf AS 10 - ,m CVCLONC
«™
— —
_
OHI6INAL MTMtl QlSH 1
IBUSH ANY FABTICULATt AO-
HIBINO TO tASKSTONTO FILTIH
COVIM SI AL ABOUND LIO
WITH TWLON«TA»f
HOUSINO
•MUSH ANY MHTICULATI AO-
HIMINO TO fmOHT MAL» ONTO
HINU f«OMT MAL^ WITH
CM,0,:CH,OM. AOO IHUIM
HINSC SACK MALf WITH
jOH MIXTUHIS Ant »-.so v/v.
ALL COMTAINIMS MM JAM»l.H KM OHQANIC ANALYSIS MUST II CLASS.
US* Tlrtl>l« OM QLASS WASH iOTTLIJ; TIFLON* IS MUMHMIO.
Figure 5-9. SASS sample handling and transfer:
and filter.
nozzle, probe, cyclones
gep.003
5-19
-------
XAO-JW
MOQUUI
INTACT SOMIENT MODULI
Am* SAMPLING HUN
MELEASS CLAM* JQININO
SOMENT CARTRIDGE
SECTION TO THE (JfftR GAS
CONOITIONIHQ SECTION
REMOVE CONOENXATE
ftUERvoiR AND DRAIN
CONOf MSATE THROUGH
VALVt INTO THE
CONOEN1ATI ORAIN
CONTAIN!m utio TO
COLUCT COWOIN«ATI
OUNINQ THI SASZ HUN
CVOJI CONOINtATI VALVt
ANO Hf ASItMILf TO MOO-
UtiTO COLLBCT WAJMINOI
MILIAM W*W CLAM*
ANO LIFT OUT INNM WILU
ANO CONOIMMH WAU.
MMOVf SOMIINT DM.
TMIOQI MOM HOUJ«H.
MIMOVI KHUN l>nOM
TO* 0» CAHTHIOai.
WWTV Hf SIN INTO A
WtOI-MOUTH AMItH JAH
HINM KHUN ANO CAM.
THIOQf INTO "HIM CON-
TAINIH WITH ex,n,
MIAtUMCLf UOOULI TO
?OU.ICT WAIMINQS
»INM WITH
UM«U Hf JIN CONTAINIH
ANO ftlNtlNO*
'LAC» INNJR rrtl.1.
Af 101 IN CUIAN AKtA
"INJI (NTHANCS TUH ANO
1ACX MALI« a* ^ILTIH MOO*.
INO INTO MODULI. HINM
00¥»N CONOCKSIM WALL
ItLIASI CINTHAU CUAHW
TO UFAMATE CONOf NSM
SICTION FROM LOW!H
SECTION. MINSI LOWM .
SECTION INTO CONOENlATt
CU*. MSLIA1I THE EOTTOM
CUUO ANO MIKIE INTO
CONOENSATS cur. OMAIN
INTO AUMM •OTTU VIA
OMAIN VAUVE
CLEAN ALL MODULE MtTAk
VAHTS tY CLEANING
Figure 5-10. SASS sample handling and transfer: organic module section.
gep.003
5-20
-------
IMPINOtft
IMPINGIft • 2
Mf AtUftf VOUIMfc H1COMO
THAN** I* CONTINTS TO
MOV/' CONTAIN!*
HINSCWITH OISTIU.ro-
OIIONIZf O MjO
TdANSMH KINSU TO
a«*ou*Tio CVUNOW.
MlASUBi VOUJMt: HICOHO
OISCAHO
WITH KNOWN AMOUNT O*
t.Wt V.«A01NO »"OM SO««1HT
Monuii TO finsr IHHNQI*
IMW1NGIK «3
MIASUMf VOLUMt: NfCOMO
i» % MOirruM aio^_ .LT™
OIKAHO
THANS«»< CONTINTS TO
CONTAIN«K
HINM WITH DISTILL!0-
OIIONIZIO MjO
THANWffl.MINIfS TO
ORAOUATtD CYLINOt«.
MIASUM VOLUUfc ntCOflO
AINM SWAOUATtD CYLINtlCH
WITH KNOW* AMOUNT 0*
OICTILLf 0-OtlONIZVD MjO
IMMNOIN '
WIKIH: flKOKO WIIOHT
OISCA^O OM HCOINtKATt
• NIGM-OtK»ITY UNtAH WUrtTHVLINt.
Figure 5-11. SASS sample handling and transfer: inipiriger train.
gep.003
5-21
-------
METALS IN SLUDGE ANALYSIS PROTOCOL
Total Metal
ICAP
Method. 6010
Sludge
Digest/gram
Aliquot by
Method 3050
AA Furnace
Pb Method 7421
As - Method 7060
Figure 5-12. Analysis protocol for metals in sludge.
gep.003
5-22
-------
METHOD 8240 - VOLATILE ORGANICS
Sludge or Ash
1
Scrubber Water
Mix .5 to 1.0 grams of solid
with 5 ml of Tetraglyme and
Place 1n Purge Vessel of
Method 624 Purge
Trap Apparatus
Transfer 5 ml Aliquot to Purge
Vessel of tho Method 624
Purge and Trap Apparatus
Add 50 ng of Internal
Standard d~ Benzene to
the Vessel
Add 50 ng of Internal
Standard d« Benzene to
the Vessel
Purge the Sample for 10 m1n.
with Inert Carrier Gas Onto
Analytical Trap of P4T
Apparatus
Purge the Sample for 10 m1n.
with Inert Carrier Gas Onto
Analytical Trap of P4T
Apparatus
Desorb the Analytical Trap
at 180°C for 5 m1n.
Desorb the Analytical Trap
at 180°C for 5 m1n.
Analyze by GC/MS
Analyze by GC/MS
Figure 5-13. Analysis protocol for volatile organic:; in solids wastes.
gep.003
5-23
-------
-------
5.6 REFERENCES
1.
2.
3.
4.
5.
6.
Method 5 - Determination of Particulate Emissions from Stationary
Sources. 40 CFR Ch. 1, .Part 60, Appendix A, Method 5. July 1, 1988.
Draft - Methodology for the Determination of Trace Metal Emissions in
Exhaust Gases from Stationary Source Combustion Processes. . U.S.
Environmental Protection Agency. Research Triangle.Park, N.C.
Sampling for the Determination of Chlorinated Organic Compounds in
Stack Emissions - Draft. American Society of Mechanical Engineers and
the U.S. Environmental Protection Agency. December 31, 1984.
Analytical Procedures to Assay Stack Effluent Samples and Residual
Combustion Products for Polvchlorinated PCDD and PCDF - Draft.
American Society of Mechanical Engineers and tha U,,S. Environmental
Protection Agency. December 31, 1984. Revised by Triangle
Laboratories - February 1989.
Volatile Organic Sampling Train. SW-846, Method 0030.
September 1986.
Revision 0.
Modified Method 5 Train and Source Assessment Sampling System
Operator's Manual. Schlickenrieder, LynnM., et'a'J. (Arthur D. Little,.
Inc.). U.S. Environmental Protection Agency. Research Triangle Park,
North Carolina. February 1985. •
gep.003
5-24
-------
-------
APPENDIX A !
U.S. SEWAGE SLUDGE INCINERATORS
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TECHNICAL REPORT DATA
(Please read Instructions on the Teverse before completing1)
1. REPORT NO.
£7^-405/2-90-009
2.
4. TITLE AND SUBTITLE
Locating And Estimating Air Toxics Emissions From' '
Sewage Sludge Incinerators
7. AUTHOR(S)
9 PERFORMING ORGANIZATION NAME AND ADDRESS
Radian Corporation
Post Office Box' 13000
Research Triangle Park. NC 27709
12. SPONSORING AGENCY NAME AND ADDRESS
U.S. Environmental Protection Agency
OAR. OAQPS, AQMD, NPPB, PCS (MD-15)
Research Triangle Park. NC 27711
3. RECIPIENT'S ACCESSION NO.
5. REPORT DATE
May 1990
8. PERFORMING ORGANIZATION CODE
90-203-080-83-02
10. PROGRAM ELEMENT NO. |
11. CONTRA CT/ GRANT NO .
68-02-4392. Work-
Assignment 52 & 83
13. TYPE OF REPORT AND PERIOD COVERED
Final. 3/89 - 11/89
14. SPONSORING AGENCY CODE
15. SUPPLEMENTARY NOTES • •
EPA Project Officer: William B. Kuykendal
" !
16 ABSTRACT This document is intended to assist groups interested in inven-
torying air emissions of various potentially toxic substances from sewage
sludge incinerators. Its intended audience includes Federal, State and local
air pollution personnel. The document presents information on the process
description of the various types of sewage sludge incinerators and their air
pollution control equipment. Emission factors are presented for each major
type of sewage sludge incinerators for the following: metals including
arsenics, beryllium, cadmium, chromium, and nickel; and organics including
chlorinated dibenzo-p-dioxins, dibenzofurans, benzene, chlorinated benzene.
and phenol. 17
a. DESCRIPTORS
Sewage Sludge Incineration
Air Toxics Emissions
Emission Factors
18. DISTRIBUTION STATEMENT
Unlimited
KEY WORDS AND DOCUMENT ANALYSIS
b. Identifiers /Open ended terms C. COSATI Field/Group
19. SECURITY CLASS (TVias Re-port) 21. NO OF PAGES
Unclassified 79
20. SECURITY CLASS (This page} 22. PRICE
Unclassified i
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