Pulp, Paper and Paperboard Industry Background Information For Proposed Air Emissions Standards Manufacturing Processes At Kraft, Sulfite, Soda and Semichemical Mills


                                      EPA-453/R-93-050a
   Pulp, Paper, and Paperboard Industry-
         Background Information for
      Proposed Air Emission Standards

         Manufacturing Processes at
Kraft, Sulfite, Soda, and Semi-Chemical Mills
                 Emission Standards Division
              U.S. ENVIRONMENTAL PROTECTION AGENCY
                   Office of Air and Radiation
               Office of Air Quality Planning and Standards
               Research Triangle Park, North Carolina 27711
                     October 1993

-------
This report has been reviewed by the Emission Standards Division
of the Office of Air Quality Planning and Standards, EPA, and
approved for publication.  Mention of trade names or commercial
products is not intended to constitute endorsement or
recommendation for use.   Copies of this report are available
through the Library Services Office (MD-35),  U.S. Environmental
Protection Agency, Research Triangle Park NC 27711, (919) 541-
2777,  or from National Technical Information Services, 5285 Port
Royal Road, Springfield VA 22161, (703) 487-4650.
                                ii

-------
                 ENVIRONMENTAL PROTECTION AGENCY

                      Background Information
                            and Draft
                  Environmental  Impact Statement
             for_Pulp,  Paper,  and Paperboard Industry

                           Prepared by:
      C. Jordan                                          (Date)
Director,^Emission Standards Division
U. S. Environmental Protection Agency
Research Triangle Park, NC  27711

1.   National emission standards for hazardous air pollutants
     (NESHAP) are being proposed for the pulp and paper industry
     under authority of Section 112(d) of the Clean Air Act as
     amended in 1990. The proposed NESHAP requires controls for
     hazardous air pollutant emissions from wood pulping and
     bleaching processes at pulp mills and integrated mills
     (i.e., mills that combine on-site production of both pulp
     and paper).

2.   Copies of this document have been sent to the following
     Federal Departments:  Labor, Health and Human Services,
     Defense, Transportation, Agriculture, Commerce, Interior,
     and Energy; the National Science Foundation; the Council on
     Environmental Quality; members of the State Territorial Air
     Pollution Program Administrators; the Association of Local
     Air Pollution Control Officials; EPA Regional
     Administrators; and other interested parties.

3.   The comment period for review of this document is 90 days
     from the date of publication of the proposed standard in the
     Federal Register.  Mr. Stephen Shedd may be contacted at
     (919)  541-5397 regarding the date of the comment period.

4.   For additional information contact:

     Mr. Stephen Shedd
     Chemicals and Petroleum Branch
     U. S.  Environmental Protection Agency
     Research Triangle Park, North Carolina  27711
     Telephone:   (919) 541-5397

5.   Copies of this document may be obtained from:

     U. S.  EPA Library (MD-35)
     Research Triangle Park, North Carolina  27711
     Telephone:   (919) 541-2777

     National Technical Information Service
     5285 Port Royal Road
     Springfield,  Virginia  22161
     Telephone:   (703) 487-4650

-------
                       TABLE OF CONTENTS


Section                                                    Page


1.0  INTRODUCTION	   1-1

     1.1  SCOPE OF THE BACKGROUND INFORMATION DOCUMENT   .   1-2

     1.2  DOCUMENT ORGANIZATION 	   1-4

2.0  PROCESS DESCRIPTIONS AND EMISSIONS ESTIMATES ....   2-1

     2.1  INDUSTRY CHARACTERIZATION 	   2-1
          2.1.1  Pulp Production	   2-1
          2.1.2  Paper Production 	   2-3

     2.2  PROCESSES AND THEIR EMISSION POINTS 	   2-5
          2.2.1  The Pulping Process	   2-5
          2.2.2  The Bleaching Process	2-22

     2.3  BASELINE EMISSIONS  	  2-30
          2.3.1  Summary of Federal Regulations 	  2-31
          2.3.2  Summary of State Regulations 	  2-31
          2.3.3  Baseline Emission Controls 	  2-34
          2.3.4  Baseline Emissions 	  2-38

     2.4  REFERENCES	2-40

3.0  EMISSION CONTROL TECHNIQUES	-. .  .   3-1

     3.1  INTRODUCTION	   3-1

     3.2  APPLICABLE CONTROL TECHNIQUES FOR VENTS ....   3-3
          3.2.1  Vent Gas Collection and Transport
                   System	   3-6
          3.2.2  Applicable Vent Control Devices  ....   3-9

     3.3  APPLICABLE CONTROL TECHNIQUES FOR
            WASTEWATER EMISSION POINTS  	  3-21
          3.3.1  Wastewater Collection System 	  3-21
          3.3.2  Steam Stripper with Vent Control ....  3-21
          3.3.3  Air Stripper with Vent Control	3-26

     3.4  REFERENCES	3-27

4.0  MODEL PROCESS UNITS,  CONTROL OPTIONS,  AND
     ENVIRONMENTAL IMPACTS  	   4-1

     4.1  MODEL PROCESS UNITS 	   4-1
          4.1.1  Pulping Model Process Units  ...  . .  .   4-2
          4.1.2  Bleaching Model Process Units  .  .  ^ .  .   4-6


                              iii

-------
                  TABLE OF CONTENTS (Continued)


Section                                                      Page


             4.1.3  Use  of Model Process Units in  Estimating
                   National  Emissions  	   4-8

        4.2   CONTROL OPTIONS	   4-9

        4.3   ENVIRONMENTAL IMPACTS	4-11
             4.3.1  Air  Impacts	4-12
             4.3.2  Energy Impacts	4-17
             4.3.3  Water Impacts	4-20
             4.3.4  Other Impacts	4-20

        4.4   REFERENCES	4-21

   5.0   ESTIMATED CONTROL COSTS   	   5-1

        5.1   CONTROL COSTS    	   5-1
             5.1.1  Enclosure Costs	   5-3
             5.1.2  Ductwork  and Conveyance  Costs   	   5-4
             5.1.3  Thermal Incineration System  Costs   .  .  .   5-7
             5.1.4  Scrubber  System Costs   	  5-12
             5.1.5  Steam Stripping Costs   	  5-18

        5.2   CONTROL OPTIONS  COSTS  	  5-21

        5.3   REFERENCES	5-34

   6.0   DATABASE SYSTEM  FOR ESTIMATING  NATIONAL  IMPACTS  .  .   6-1

        6.1   DATA INPUTS	   6-1

        6.2   CALCULATION OF NATIONAL EMISSIONS AND
             CONTROL IMPACTS  	   6-3

        6.3   GENERATION  OF SUMMARY  OUTPUT  FILES   	   6-4

        6.4   REFERENCES	   6-5

   APPENDIX  A      	   A-l

   APPENDIX  B	   B-l

   APPENDIX  C	   C-l
                                 IV

-------
                         LIST OF TABLES


Table                                                      Page


2-1  DISTRIBUTION OF CHEMICAL AND SEMI-CHEMICAL  PULP
       PROCESSES IN THE UNITED  STATES  	   2-4

2-2  MAJOR HAZARDOUS AIR POLLUTANTS EMITTED  FROM PROCESS
       POINTS	   2-6

2-3  TYPICAL VENT AND WASTEWATER STREAM  CHARACTERISTICS
       FOR KRAFT PULPING EMISSION POINTS	"...  2-10

2-4  TYPICAL UNCONTROLLED EMISSION FACTORS FOR KRAFT
        PULPING FACILITIES   	  2-11

2-5  COMPARISON OF COMMON CHEMICALS USED IN  PULP
        BLEACHING	2-23

2-6  MOST COMMON KRAFT BLEACH SEQUENCES  	  2-26

2-7  TYPICAL VENT AND WASTEWATER STREAM  CHARACTERISTICS
       FOR KRAFT BLEACH PLANT EMISSION POINTS  	  2-27

2-8  SUMMARY OF TYPICAL UNCONTROLLED EMISSION FACTORS
       FOR KRAFT BLEACH PLANT FACILITIES  	  2-28

2-9  SUMMARY OF FEDERAL REGULATIONS (NSPS) FOR EMISSIONS
       FROM KRAFT PULPING FACILITIES   	  2-32

2-10 SUMMARY OF STATE REGULATIONS FOR  EMISSIONS  FROM
       PULPING FACILITIES 	  2-33

2-11 SUMMARY OF EXISTING TECHNIQUES TO CONTROL
       HAP EMISSIONS FROM PULPING VENT SOURCES	2-35

2-12 SUMMARY OF EXISTING TECHNIQUES TO CONTROL
       HAP EMISSIONS FROM BLEACH VENT  SOURCES	2-36

2-13 SUMMARY OF ADD-ON CONTROL  STATUS  OF WASTEWATER
       EMISSION SOURCES 	  2-37

2-14 SUMMARY OF ESTIMATED NATIONAL BASELINE  EMISSIONS
       FROM CHEMICAL AND SEMI-CHEMICAL PULPING AND
       BLEACHING OPERATIONS  	  2-39

3-1  PULPING PROCESS MODIFICATIONS AND BLEACHING
       PROCESS SUBSTITUTIONS  	 ...   3-2

3-2  PERCENT OF KRAFT MILLS USING COMBUSTION CONTROL
       DEVICES	   3-4

-------
                  LIST OF TABLES  (Continued)


Table
3-3  TYPICAL VENT CHARACTERISTICS FOR KRAFT PULPING
       EMISSION POINTS  	   3-5

3-4  SCRUBBER REDUCTION ESTIMATES 	  .  3-20

3-5  STEAM STRIPPER REMOVAL EFFICIENCIES   	  3-25

4-1  PULPING PROCESS CHARACTERISTICS AFFECTING
       EMISSIONS	   4-3

4-2  PULPING MODEL PROCESS UNITS  	   4-4

4-3  BLEACHING MODEL PROCESS UNITS  	   4-7

4-4  SELECTED CONTROL OPTIONS AND CONTROL TECHNOLOGY-
       EFFICIENCY 	4-10

4-5  UNCONTROLLED EMISSIONS FOR AN EXAMPLE FACILITY  .  .  .  4-13

4-6  PRIMARY AIR IMPACTS FOR AN EXAMPLE MILL	4-14

4-7  EXAMPLE MILL SECONDARY AIR POLLUTION IMPACTS  ....  4-16

4-8  EXAMPLE MILL ENERGY IMPACTS  	  4-19

5-1  ELEMENTS INCLUDED IN CONTROL COST CALCULATIONS
        FOR VARIOUS POINTS/DEVICES  	   5-2

5-2  DUCTWORK GENERAL DESIGN SPECIFICATIONS FOR VENTING
       TO AN EXISTING COMBUSTION DEVICE 	   5-5

5-3  THERMAL INCINERATOR GENERAL DESIGN SPECIFICATIONS
       FOR HALOGENATED VENT STREAMS	   5-8

5-4  DESIGN PARAMETERS FOR POST INCINERATION
       SCRUBBER SYSTEM  	  5-14

5-5  DESIGN PARAMETERS FOR STAND-ALONE SCRUBBER SYSTEM   .  5-16

5-6  STAINLESS STEEL COST FACTORS 	  5-22

5-7  SUMMARY OF COSTS FOR CONTROL OPTIONS FOR  AN
       EXAMPLE FACILITY	5-23

5-8  COST FOR MODEL MILL PULPING VENTS NOT REQUIRING
       ENCLOSURES USING AN EXISTING COMBUSTION DEVICE .  .  5-25
                               vi

-------
                  LIST OF TABLES  (Continued)


Table                                                      page


5-9  COSTS FOR MODEL MILL PULPING VENTS REQUIRING
       ENCLOSURES (FUGITIVE SOURCES) USING AN EXISTING
       COMBUSTION DEVICE  	  5-26

5-10 COSTS FOR CONTROL OF MODEL MILL BLEACHING VENT
       STREAMS USING A STAND-ALONE SCRUBBER 	  5-27

5-11 COSTS FOR CONTROL OF MODEL MILL BLEACHING VENT
       STREAMS USING AN INCINERATOR FOLLOWED BY
       A SCRUBBER	5-28

5-12 COST FOR CONTROL OF MODEL MILL PULPING WASTEWATER
       STREAMS USING A STEAM STRIPPER 	  5-30

5-13 COMPARISON OF TOTAL CAPITAL INVESTMENT (TCI) AND
       TOTAL ANNUAL COST (TAG) FOR MODEL MILLS WITH
       VARYING CAPACITIES 	  5-33
                              vii

-------
                        LIST OF FIGURES


Figure                                                    page

1-1  Segment of pulp and paper industry discussed
       in this document	   1-3

2-1  Percentage of wood pulp produced by each process .  .   2-2

2-2  Breakdown of emission points in typical kraft
       pulping and bleaching processes  	   2-7

2-3  Typical kraft process with chemical recovery
       practices	   2-9

2-4  Typical sulfite pulping process practicing chemical
       recovery	2-18

2-5  Typical neutral sulfite semi-chemical pulping
       process	2-20

2-6  Typical down-flow bleach tower and washer  	 2-24

3-1  Discrete burner, thermal incinerator 	 .  . 3-14

3-2  Packed tower absorption process  	 3-18

3-3  Continuous integrated steam stripper system  .... 3-23

4-1  Example air pollution impacts  	 4-18

6-1  National impacts estimation process  	   6-2
                             Vlll

-------
                       1.0  INTRODUCTION
    ' National emission standards for hazardous air pollutants
 (NESHAP) are under development for the pulp and paper industry
under authority of Section 112(d) of the Clean Air Act as
amended in 1990.  This background information document (BID)
provides technical information and analyses used in "the
development of the proposed pulp and paper NESHAP.  Effluent
guidelines limitations for pulp and paper mills are being
developed concurrently under the Clean Water Act.  The U. S.
Environmental Protection Agency  (EPA) is coordinating these
efforts to produce integrated decision-making for the air and
water regulations for the pulp and paper industry.  Technical
information used for the development of effluent guidelines
limitations is in separate documents.  However, this BID does
include air emission impact factors for the process technology
options considered for establishing effluent guidelines
limitations.
     The EPA has conducted a number of public meetings to
review and discuss the technical approach to developing these
joint air and water regulations.  An April 1994 preliminary
draft of this document was reviewed by the public.  All of the
comments received on the preliminary draft, in addition to
information provided at the public meetings, were reviewed and
considered in revising this document.  Comments and
corrections were incorporated into the BID to ensure that the
BID is technically accurate and describes the Agency's
documented conclusions about the control technologies,
emission factors, control costs, and other impacts upon which
the proposed rule is based.  Comments and data received that
modify the proposal analyses were considered and evaluated to
                              1-1

-------
determine the impact on proposal,  but they were not
incorporated into the proposal's analyses or this document.
The EPA will continue to evaluate those comments and data,
along with other public comments received on the proposed
rule, and all comments will be considered in the development
of the final NESHAP.
1.1  SCOPE OF THE BACKGROUND INFORMATION DOCUMENT
     The scope of this document covers wood pulping and
bleaching processes at pulp mills and integrated mills (mills
that combine on-site production of both pulp and paper).   Such
mills would typically fall under standard industrial
classification codes 2611 and 2621, respectively.  Figure 1-1
provides an overview of the pulp and paper industry and
identifies the segment of 'the industry discussed in this
document.  Detailed information about the production of paper
(at integrated or non-integrated mills) is not included in
this document.  The secondary fibers segment of the industry,
which consists of mills that manufacture pulp from recycled
paper products, is also not included.
       The pulping process is designed to separate the
cellulose fibers in the wood chips.  Pulp mills and integrated
mills use a variety of methods to pulp wood.  The three main
types of pulping processes are chemical, semi-chemical, and
mechanical.  Chemical pulping is the most common of the three
pulping processes.  Chemical and semi-chemical pulping
processes are the focus of this BID.  Mechanical pulping
processes are not included.
     As shown in Figure 1-1, chemical and semi-chemical
pulping processes are divided into two groups:  process
operations and chemical recovery.  Air emissions from process
operations are discussed  in detail in this BID; emissions from
the chemical recovery process will be evaluated at a later
date in  separate documents.  The process operations covered
in this BID include the pulping of wood chips, evaporation of
weak spent cooking  liquor, and pulp bleaching.  Chemical
recovery operations  (not  included in this document) include
                              1-2

-------
the equipment used to recover the cooking chemicals from the
strong spent cooking liquor.
     The purpose of this BID is to document the Agency's
conclusions about hazardous air pollutant (HAP) emissions from
this industry, the demonstrated technologies available to
control HAP emissions, and the costs and other impacts of
applying these technologies.  Regulatory alternatives and the
national environmental and cost impacts will be presented in
other EPA documents.
1.2  DOCUMENT ORGANIZATION
     Chapter 2.0 presents an overview of the pulp and paper
industry, including process descriptions, air emission points,
and estimated national baseline emissions.  Control
technologies are discussed in Chapter 3.0.  The model process
units that were developed to estimate the regulatory impacts
on the industry are discussed in Chapter 4.0, along with
options for controlling HAP emissions from pulping and
bleaching vents and wastewater streams.  Example environmental
impacts are also shown in Chapter 4.0.  Costs for controlling
HAP emissions from the various emission points in the pulp and
paper industry are discussed in Chapter 5.0.  Chapter 6.0
gives a brief overview of the data base developed to estimate
national environmental and cost impacts for the pulp and paper
industry discussed above.  The appendices include Field Test
Data (Appendix A), Air Emission Estimates and Emission Factors
Development (Appendix B), and Model Process Units
(Appendix C).
                              1-4

-------
       2.0  PROCESS DESCRIPTIONS AND EMISSIONS ESTIMATES

     This chapter presents an overview of the pulp and paper
industry, focusing on the chemical pulping and bleaching
processes used in the industry.  Section 2.1 describes the
character and distribution of pulp and paper mills in the
United States; Section 2.2 discusses unit processes and their
emission points; and Section 2.3 describes baseline emissions
and control technologies.
2.1  INDUSTRY CHARACTERIZATION
     The pulp and paper industry includes facilities that
manufacture pulp, paper, or other products from pulp.
Converting operations such as the production of paperboard
products  (e.g., containers and boxes) and coating or
laminating are not included in the pulp and paper industry.
     Based on responses to a 1992 EPA Office of Water survey
(which are considered Confidential Business Information),1
there are 565 operating pulp and paper facilities in the
United States.  Many of these pulp and paper facilities
operate more than one type of pulping process; for example,
they may produce pulps using a chemical (e.g., kraft-or
sulfite) process and a mechanical or semi-chemical process.
Based on this survey, there are 253 wood pulping processes
(chemical, semi-chemical, and mechanical)  operating in the
industry.
2.1.1  Pulp Production
     Although other raw materials can be used, the material
most commonly used in the manufacture of pulp is wood.  Based
on 1992 estimates, approximately 71.8 million tons of wood
pulp are produced annually in the United States.1  Figure 2-1
illustrates the percentage of wood pulp produced in the United
States by each pulping process and the approximate number of
                              2-1

-------
•a
o
o
o
o
9
+•>
§
o
I
    100
     90  —
     80  —
     TO  —
     60  —
     60  —
40 -
     30  —
     2O  —
     1O  —
                 84.0%
                                           Note: Mills Producing More
                                               Than One Pulp Type
                                               Are Counted Once
                                               For Each Type.
               (149)
              Kraft ft Soda
                         SiMto
  Figure 2-1. Percentage of Wood Pulp Produced by Each Process    i;
                                    2-2

-------
mills of each type.  The pulping processes discussed in this
document (kraft, soda, sulfite, and semi-chemical)  account for
approximately 68.4 million tons or 95 percent of total U.S.
wood pulp production and are present at 161 mills that are
being considered for the NESHAP supported by this document.
Table 2-1 shows the distribution of the 565 mills in each
State by type of chemical or semi-chemical pulping process
used.2  The States with the highest concentration of chemical
pulp mills are Washington, Alabama, and Georgia.
     Kraft (including soda) pulp production accounts for
approximately 85 percent of U.S. wood pulp production.1'3
There are approximately 149 kraft pulping processes,1 located
primarily in the southeastern United States.  This region
provides over 60 percent of the wood pulp in the United
States.3
     Figure 2-1 also shows that there are currently 16 sulfite
pulping processes in the United States, which contribute
approximately 4.percent of total U.S. wood pulp production.1
The majority of sulfite mills are located in the north and
northwest,  where the softwood species used in sulfite pulping
(spruce, hemlock, and fir) are more prevalent.  However,
sulfite pulp can also be produced using hardwoods such as
poplar and eucalyptus.4
     Approximately 32 pulping processes in the United States
use semi-chemical pulping, which contributes approximately
6 percent of nationwide wood pulp production.1/3  There is no
geographic concentration of mills employing semi-chemical
pulping technology because the technology can use a wide
variety of wood species and, thus, is not restricted to a
given region of the country.
2.1.2  Paper Production
     According to the 1991 Lockwood-Post's Directory for Pulp,
Paper and Allied Trades, approximately 38.7 million short tons
of paper were produced in the United States in 1991.5  Based
on responses to the 1992 EPA Office of..Water survey, 	
                              2-3

-------
 TABLE 2-1.  DISTRIBUTION OP CHEMICAL AND SEMI-CHEMICAL
               PULP PROCESSES IN THE UNITED STATES*/b
State
Alabama
Alaska
Arizona
Arkansas
California
Florida
Georgia
Idaho
Indiana
Iowa
Kentucky
Louisiana
Maine
Maryland
Michigan
Minnesota
Mississippi
Montana
New Hampshire
New York
North Carolina
Ohio
Oklahoma
Oregon
Pennsylvania
South Carolina
Tennessee
Texas
Virginia
Washington
Wisconsin
Total
a Based on Reference
b Mills producing moi
Kraft/soda
16

2
7
3
11
13
1


2
11
8
1
3
3
5
2
2
1
7
1
1
7
4
6
3
8
5
12
4
149
2.
re than one pi
Sulfite Semi-chemical
2
2



1
1

1
1
1
3
1

3



1
1 2
1
2
1
3
1
1
1

3
5 3
5 2
16 32

ulp process are counted or
for each pulp process,
                           2-4

-------
integrated mills accounted for 25 percent of production, non-
integrated mills for approximately 10 percent,1 and secondary
fiber mills for approximately 65 percent.1
2.2  PROCESSES AND THEIR EMISSION POINTS
     This section provides a detailed discussion of process
emission points for chemical and semi-chemical mills pulping
wood, as well as the specific HAP's emitted from these points.
Industry review of the emission factors presented in this
section suggests that further testing be conducted to
supplement existing data.  Industry has provided some
emissions data and is currently testing several pulp mills.
These and any additional test data provided to the EPA will be
considered for review and for incorporation into the final
regulatory analysis.
     A list of HAP's associated with process emission points
is given in Table 2-2.  As discussed in Chapter 1.0, the scope
of this document is limited to points referred to as process
operation points.  Included in this group of points are the
digester system, the knotter, the washer system, the
evaporator system (in the chemical recovery area), coproduct
recovery, and the bleaching process.  Figure 2-2 provides a
flow diagram of a typical kraft pulping operation and depicts
process operations and chemical recovery points.  Chemical
recovery air emission points (other than the evaporator
system) will be discussed in future documents.
     The pulp production can be divided into two steps:  the
pulping process and the bleaching process.  The exact
processes used for pulping and bleaching depend on the end use
of the pulp.
2.2.1  The Pulping Process
     The pulping processes discussed in this document are
kraft, sulfite, semi-chemical,  and soda.  Detailed
documentation of the differences between the kraft and soda,
sulfite,  and semi-chemical pulping processes was provided by
the industry.   These differences are being considered in the
                              2-5

-------
TABLE 2-2.  MAJOR HAZARDOUS AIR POLLUTANTS EMITTED FROM
                        PROCESS POINTS
                     Chemical name

                 1,4-Dichlorobenzene
                 2,4,5-Trichlorophenol
                 2-Butanone  (MEK)
                 Acetaldehyde
                 Acetophenone
                 Acrolein
                 Carbon disulfide
                 Carbon tetrachloride
                 Chlorine
                 Chloroform
                 Formaldehyde
                 Hexane
                 Hydrochloric Acid
                 Methanol
                 Methyl chloroform
                 Methylene chloride
                 Propionaldehyde
                 Toluene
                           2-6

-------
                                              UlOlBZZi
>
1
o
0)
QC
15
.0
»










• ^^
§5
. S-52
£.c
o *-
5->
O.o
WQ
CO 0}
0) h.
o 9
o 2
«- °
s



r 	

-St. -53J5
I'ifslS!
1 5§Jl|gs
- 1 " S--S g s
l!!1!!!

t



1
1 '
2-g* "
HI 5

1
i
4
'

1
1 a ^
5^|
1 	


- —







fe§
$SS
S|l
Hi
S O°
11


Recovery

r~
i
Is

• • —
Coproduot
Recovery

i

. M 1 . H Jl. in
Hi! IV
o0- ,g

	 (_.
.-•L- _^^I^
• ?= « £
0> -g fl> Q.
•s f Silt
Is £i<3*
1| ^^«
»* 1
t -
J -1
J J
§ 1
o-
3
1
I
5I
1
__ J 	
1
a. a. a. i
2 g If S •
. z* r 3« . *
J* J* [«_
	 1 	 I_ 	











(
<
1
<
I S
Q - S 0
Z W i: -
I" « W
S i •
2 o- j
ft *"1 t
I
1

o
g
•o
1
.S
1
S c 1
5 « S
>5I .5
S — "°
-*ll s
if i
« 1
•
«
c
I
-s










D
)
C
>.
>
>
J
g
1
1



w
o
1
^
a
A
1
I
ration of
•

                                                       Q)

                                                    W  «

                                                    c  ®
                                                   .=  o
                                                    o  o
                                                    O   °>

                                                   '35  ~

                                                   .£2  -c

                                                   1   ro
                                                   n i   0)

                                                   «-  m
                                                    o  ^

                                                    c   c

                                                    $   ra
                                                    O   O)



                                                   "ro  !§•
                                                    rtj   *^


                                                   m  °-
                                                       4-<


                                                   oil

                                                   cs  ^

                                                    0)   (0
                                                    b:   U
2-7

-------
rule; however, they are not included specifically in this
document.
     The remainder of this section discusses these three
pulping processes and their emission points.  Despite their
differences, all three pulping processes begin with the
preparation of wood into wood chips.  Wood chips are sent
through a digestion process to chemically reduce the chips
into a pulp.  The pulp then goes through several steps where
knots and oversize particles and spent chemicals from the
digestion process are removed from the pulp.  Some pulping
processes, such as kraft, recover the spent chemicals for
reuse in the pulping process.  The remainder of this section
discusses these three pulping processes and their emission
points.
     2.2.1.1  The Kraft Process.  Figure 2-3 presents a
typical kraft pulping process, with the emission points
identified.  Table 2-3 presents the vent and wastewater stream
characteristics and the HAP emission characteristics, for the
emission points shown in Figure 2-3.1/3/6/7  Table 2-4
presents emission factors for these points.  Emission factor
ranges are given in Table 2-4 for the various emission points.
Table 2-4 provides only a summary of the emission factors
developed and shown in Appendix B.  In most cases, the
emission factors presented in Table 2-4 are of the same order
of magnitude as those supplied by industry in June 1993 (NCASI
technical bulletin 650).
     The key components of the kraft pulping process, as shown
in Figure 2-3, are digestion, deknotting, brownstock washing,
screening, chemical recovery, and coproduct recovery.  The
kraft pulping process involves cooking wood chips in a white
liquor solution of sodium hydroxide and sodium sulfide.  This
cooking or digestion process breaks down the wood structure by
dissolving the lignin that holds the wood fibers together.
The digestion process produces unbleached pulp (brownstock)
and weak black liquor, which is a solution of solubilized
lignin, water, hydrolysis salts, and sulphonation products.8
                              2-8

-------
                                           U9118ZZI





a
z
UJ
O




1
"5
oc
^ ^^
3 o
.•ge
"'«
o g
DB JE '
W Cl






§~

: Z o
"S ~ E «S
O • «• •• (A
Hill
o

1
1
a a
£ «
II
o £
I— H-









                                                  CO
                                                  
-------
^3 *^
~ s
4-1 C U
<0 01 
P4 J>~
O
MM
CQ x
CJ -g
H "^
* ~o 3
M 52 a.
S =s»
H 1
0 8
|ffi ^
fyj
i3
9 «^> >.

JO 2 'o ^
•— &« «» s H-
*§ £ £ 9-9
jrf !•«< < CO ^

« 2
-, O •- 'o •S
K S x 5 •-
B« *h
J2 LJ
M 5J 0 »%
^'^ &1 ff ^* ^"*
CO 1~ -8
^£ '? 5 I™
& "- co §
•* X o V*
Q
2
*

W .S
> 8.
J §
fffi **T
Li: M
U W)
S a
JH

*
7 |w
CJ <" .5 o
'g a.

j
0)
b i
EH .2 w
.2 '5
CB Q-
IB ^^
UJ


0
o
O .n ^ O O
N. X> ?. «. «,


8: ° s « 2
S ifi « s ~


in ^ in in
jvl y ivi to jvj
CO «_ >!• Kl





•o S
«. g | ^ *
- o 5 ° °





o o o o o
(vi (vi (vt IM m




§o o o in
O O O (VI




s s s § s




"
g i X
OI ^ O

2 !r « «
1 2 si
£ .? .2 *

01 (fl U O
oi 3 je ^
^ 1 S fc? c.
j: .— «i w 01 01
O 4-» 41 4-f 41 £
w CM o» Q i. M
0 U D) Q ^ M 3



•- (vi to •* in







•^



0 '





0 O
in (vi
-











o
*-


^




5






-o
(VI
o
0





o
to
0



§
to




§
^*




s

gnificat

«1
g w
23
.33



00










O O Q ^
O fO^CO°2 << < ^
sf z 2 ~ ~ z °
1
s.
§ «
z izzzz zz z- -o
"* o
3
§
i/t in ^ S
S~~(v;55S53 |
^ ^ •*
x a
>
i M
to c
>O 00
r~ >p —
O IS. 4J
h-N.1"-"-*^ 0 -0™
2 SSg?g T^ ^ § S
0 §. ° § S § g 0 ~ 0 S
0 ° « § ° o * :-. §
° PJ 41
0 ^ S
Vt 4-*
ID C
OI 01
X fj
o o o o o o oo o a ^-
to in(vi(vi(viin (vi(vi in *4-
o "ON-N-rs-*o r*.N- ^o o •

C 41
O 1-
ginoomin oo in 041
(VIOO(VI(VI OO (M O >
tO -O CO CO ^O -O CO CO ^inin >t^ in **roc
O4 ^O O^ O* ^O ^O O^ O* ^3 L. (0
^ o Tp oi
"5 4-> o
L.
•^ (U 4-1
(_ u
(11 tA 41 ^Q
ra S «- <- _
a 4J •- t.C4'cr o e i-o 4>
C 0) 0 4J O 0 — 341 5 0—3
OIIA^MUfO-' 0*0 U ^U.—'
•^ *s* 41 ~ * (0
— °DU4l4li-.k< ^41 u >
4ico4-ic o clo —*'.,'.—,:;
•D(04^ — — 41 4-— (0 «,T,eC:^
o) .c a- "D a. — ^ j* 41 a.41 a. 5- " ,. 55
x— 3 LU ^"'Sai^
41 . j; 4-
K ^~ 4^ 4>* O
§M M —
41 41 •» 4->
o. o^(vito>» in* h. igS^S
CJ (0 C
01 1. — 01 01
I- 41 — 4J M
(0 S- (0 C 41
41 > O .C
M ae  4-> 41
"J 4- 5 O (0 M
t£ — Z 41 10
S U Tl £ 41
3 g 5 II <-
41 O. M 41 U
% (0 <0 < f C
« 
-------



V>
Of
t—



0)
^\ L)
a <
I
0)
x
Ol
^
%^
41 £
o> 2
S €
2 o;
c.
o
*J
CO
go
y
(A *
g --*
Ul 4J
£



U
a.


"«

O






Emission point





§2

i c

'i'o
ui a.

§4.
— O
at 3
... Q
E S
Ul



CM
O
^
to

CM

ID
O
O
o



J"
°
d
(VI
§
o
d



>»
^^
i
CM






^*
d








CO
a>
c_
0)
tfl
O)
'•5
f.
u
CO
CO




.-






1



o
»J.
>»
(M

CM
8
o
o
'3
o
8
O




i
|i



o

1




o
0
8

o
in
ro
0
§
0



(A
10
O)
1
L.
41
Ol
|
•W
4-*
§
u




CM










N.
IM
•O
CM


-O
8
8
o





o
o
o



h.
(M
•i
CM






o
o








at
(0
O)
I.
41
U)
41
D)
Q




K)








V)
0
u
*^ 10
^ tM Jvi ^ • ^ d* W* rf f*- ® N> ?•* CM >O *^
^ -* o z z z "z~dzoci52 .1

1
N M °
8 8 g § J. ^ 5 | S § J
0 <=> 0 0 0 R N-<8<°c>0?° °
i i i i 2 5 I • 2 • 8 1 2 | j |
° o ° ° ° • o o -°
'£
10
^
IA FO CM 01
o*^£o° ° *^t> oS •£
oo«-oSCoo o' o*~ *~H «
d °. =; °. 5 =: d d d °. « .
O 0 ° 0 ° Q. (0
l- O
CA U
S, 42
M ">0>t«-~C^
>o>»cog -* *^^g;ro-d 41 'w
cbcbijLcJo' '1-z-»'SS-»df:-':- o!-2
0 -^ -' ° M 00^ ". ". f|
d d ° ° ° o
CO >
X "D
•Q S
^sil s ^ss^ i i

^I^OOfO itf^rfl^U^^I
A ^ d g i 0- ozSz52o'l::?i -HS
o°oo ° °*^ *^° c~
0 o o ° 0° °0 01 '>
OT C
41 ""
CO O
~ -x "S -S3 i
«l C <0 ^ ~
C (0 Jf C • (A
01 4-» L. C 2 3 U
41 41 10 O U O O
1- 3J= 4^—41 Q.Xf
O O Ul t- Ul S •— «
M -* _U)I--C ° ^2 _
C J2 3 0) 01 41 41 ° f S
X 10 ra « -n -n qjo
t- 4-> CC .l-IOCCAC C 4-1 U £ < *
a co 4^4^ c.41 u)4it-ra 4^(A
u O to CO . — * 4> IA "04)1041 °A
> TZ ^^ St-r-goioi-n-S Isf
\^ C .^— 4-'C-C4-'O' UCt- (OOlt-
COCCC O4-'OO'^34»O3 >(0
"n 410101 fviuia— *o~ouui oi**-
O — ' 01 >*II> •" ^« 01 —* Ul * U) O) (fl
f Uo'Jl'JIjiOWC o COO*-> iftAO*
U >^ (0(OU)4-'<»-— «4I4-'CO(0(A CUE
4^4141414101 OOI4)  QO4I Tt0^'*'*'
*j _c -c ^ o> 01— a. ~o a. — ^ XX4I>O31041'-D >>O '""al.S""

CO*T3v)4-'
O 4-1 O Ul
0 S '— 4->
C (0 E 10
X H- 41 S
o jr o»

•- JC > W
41 (A 4-> — •
c_ tA '^ "D •«-
10 — 3 C 10
E a >
« 1 « 1 1 «
*o "u •** *u Z
?. 10 o o 1o u
~ a. 4i w v
71 CO Q. tfl O <
g (j in (0 t- z
« A U *O
2-11
-------
     The pulp and spent chemical slurry from the digester pass
through a knotter, which removes oversize or undigested wood.
The spent chemicals are then removed from the pulp in the    :
washing process and are recovered for reuse in the chemical
recovery process.  The pulp is then screened to remove
additional oversize wood particles and excess water is removed
in the decker.  In some processes, the pulp undergoes oxygen
delignification to remove additional lignin prior to storage
or bleaching.  The following sections describe digestion,
deknotting, brownstock washing, oxygen delignification,
evaporation, and coproduct recovery.
     2.2.1.1.1  Digester system.  The digester system, which
may be a batch or continuous process, is one of the key
components in the pulping process and generally comprises a
digester and blow tank or similar vessel.  After cooking is
completed in the digester, the weak black liquor and pulp are
discharged into a low-pressure vessel typically called a blow
tank.  Heat recovery from the blow tank gases is often part of
the blow tank system.
     Blow gases may be vented to an accumulator or a vapor
sphere for collection.  Based on the total reduced sulfur
(TRS) and terpene concentrations of the blow gas emissions,
the gases may then be incinerated, stripped, or condensed for
the recovery of turpentine.  (The processes for recovering
coproducts from digestion are discussed in Section 2.2.1.1.6)
The pulp from the blow tank may then enter a defibering or
deknotting stage prior to pulp washing to produce a higher-
quality chemical pulp.
     Because digester blow gas emissions differ between batch
and continuous digesters, two emission point identifiers are
shown in Figure 2-3 for digester blow gases (emission point
ID's 1 and 2).  Specifically, the batch digester releases
gases in surges when the digester blows its entire I'oad into a
blow tank; continuous digester emissions are released at a
constant rate.  Thus, overall volumes of gases from continuous
digesters are less than those from batch digesters.  High-
                             2-12
-------
pressure gases from the blow tank are typically sent to a
primary condenser and then to an accumulator.  The accumulator
discharges foul condensate and blow gas.  Vapors from the blow
tank are recovered and condensed to recover some of the
organic compounds.
     Digester relief gases are also a point of potential
emissions (emission point ID 3).  However, as shown in
Figure 2-3, relief gases from the pulping of softwoods can be
condensed and retained to recover turpentine (see Section
2.2.1.1.6).7
     A wide variety of volatile organic compounds (VOC) and
reduced sulfur compound emissions are produced by the
digestion process.  In addition to HAP emissions from process
vents, the wastewater produced by the digestion process
(digester blow condensates, turpentine decanter underflows,
and evaporator condensates) is a point of HAP emissions
(predominantly methanol, as shown in Table 2-4, [emission
point ID's 15, 16, 17, and 18]).
     2.2.1.1.2  Deknotting process.  The next step in the
kraft process is often deknotting, as shown in Figure 2-3.-
Knots are large pieces of fiber bundles or wood that were not
fully broken down during digestion.  They are generally
defined as the fraction of pulp that is retained (as" wood
chips or fiber bundles)  on a 3/8-inch perforated plate.9
Knots are removed from the pulp prior to washing and are
either discarded as waste, burned, or returned to the digester
for further digestion.
     Two types of knotters are in current use.   One type, an
older design, is the open-top vibratory screen.  The vibratory
screen, which releases emissions directly to the atmosphere,
is being phased out because of the large quantity of foam
generated, which lowers the efficiency of the brownstock
washer.10  Emission factors for vibratory screen knotters
are shown in Table 2-4.
     The second type of knotter consists of a totally
enclosed,  pressurized, cylindrical, perforated screen.   A
                             2-13
-------
rotating foil in this type of knotter produces a series of
vacuum and pressure pulses, which keeps the perforations clean
and reduces foam buildup.  Lower emissions are associated with
this second type of knotter because it is an enclosed system.
     2.2.1.1.3  Brownstock washing.  Pulp from the blow tank
and knotter is washed with water in a process commonly called
brownstock washing, as shown in Figure 2-3.  The purpose of
washing is to remove weak black liquor from the pulp to
recover sodium and sulfur and to avoid contamination during
subsequent processing steps.  The most common type of washer
used in the industry is the rotary vacuum washer.  Other types
of washers include diffusion washers, rotary pressure washers,
horizontal belt washers, wash press, and dilution/extraction.
     Washers differ according to the method used to separate
black liquor from brownstock pulp.  All washers require the
addition of water  (fresh or recycled) to rinse the pulp and
recover the black liquor.  The rinsed pulp is screened for
oversize particles and thickened in a decker (emission point
ID 7), where excess water is removed prior to oxygen
delignification, bleaching, or storage.  The diluted or "weak"
black liquor is recovered in filtrate tanks and sent to the
chemical recovery process.
     A foam tank is typically used to capture the foam
separated in the filtrate tanks.  Foam is formed when soap,
which is dissolved by the caustic cooking liquors, goes
through the washing process.  If foam remains with the pulp,
it can saponify and form "pellets" on wood that are extremely
hard to disperse in the washing process, thereby reducing the
washing efficiency.11  Generally, defoaming is completed in
the foam tank using centrifugal or mechanical force to break
up the foamed mass.  This force allows air trapped in the foam
mass to vent to the atmosphere, as shown in Figure 2-3 and
Tables 2-3 and 2-4 (emission point ID 6).  The defoamed weak
black liquor is typically piped to the chemical recovery
process.
                             2-14
-------
     Emissions occur from the washing process as HAP compounds
entrained in the pulp and black liquor slurry volatilize.  The
typical vent and stream characteristics and HAP emission
characteristics of the brownstock washer are summarized in
Tables 2-3 and 2-4, respectively (emission point ID 5).   As
with the digestion process, the quantity and type of emissions
from a brownstock washer are a function of the pulp
production, type of digestion (batch or continuous), and the
type of wood pulped (softwood or hardwood), and also the point
of shower water.  Vent streams from washers are considerably
lower in temperature and in moisture content than digester
streams.  The heat content of the brownstock washer vent
varies with the type of enclosure used on the washer.
     Washers such as the rotary vacuum drum washer are
typically hooded and,  therefore, not fully enclosed.  These
washers require large volumes of air to capture and vent
moisture and fugitive emissions and, consequently, will have a
dilute HAP concentration (and thus a lower heat content).
Washers such as the diffusion washer or horizontal belt washer
are enclosed or have limited exposure to ambient air.  Vent
streams from these washers, therefore, will have lower flow
rates with higher HAP concentrations.
     2.2.1.1.4  Oxygen deliqnification stage.  Treatment of
pulp with oxygen is used in some cases as a delignification
step prior to bleaching; however, it may also be used for
bleaching in alkaline conditions.  Oxygen delignification,
when used as a step prior to bleaching with chlorine
chemicals, can help reduce bleach plant chemical use by
removing more of the lignin from the pulp.  In addition, the
oxygen delignification stage effluent is compatible with the
kraft chemical recovery process.12  Because the resulting
effluent can be recycled to the chemical recovery system,
organic loading in the bleach plant wastewater is reduced.12
Vent stream characteristics and HAP emission factors for the
oxygen delignification stage are presented in Tables 2-3 and
2-4, respectively.
                             2-15
-------
     2.2.1.1.5  Chemical recovery.  An essential element in
the kraft pulp process is the recovery of sodium and sulfur
from the weak black liquor recovered from brownstock washing
and oxygen delignification processes, as shown in Figure 2-3.
The general steps in the recovery of cooking chemicals (as
shown in Figure 2-2) are evaporation or concentration, black
liquor oxidation (optional),  combustion/oxidation/reduction
(recovery furnace), and recausticizing and calcining.  This
section only discusses evaporation; the remaining chemical
recovery processes will be discussed in future documents.
     For efficient chemical recovery of the Inorganic
chemicals, the evaporation of excess water is required.  Large
amounts of water (5 to 7 kilograms of water per kilogram of
dry solids) are evaporated to achieve a desired black liquor
solids concentration of 60 to 65 percent.13  The water is
typically removed from the spent cooking liquor in multiple-
effect evaporators, which comprise a series of direct or
indirect contact evaporators operated at different pressures
so that the vapor from one evaporator body becomes the steam
supply to the next evaporator.
     Hazardous air pollutants are emitted from the evaporation
process by two basic mechanisms.  Non-condensible gases
containing HAP's that have been vaporized during the process
of concentrating the cooking liquor are emitted from the
evaporator vents and hotwells.  Hazardous air pollutant
emissions also occur from the evaporator condensate streams
because of the partitioning of certain compounds to the air
from the liquid phase. These points are depicted in Figure 2-3
and Tables 2-3 and 2-4 (emission point ID's 10, 17, and 18).
     2.2.1.1.6  Coproduct recovery.  The kraft pulping process
produces two saleable coproducts:  turpentine and soap (tall
oil).  Turpentine is recovered from digester relief gases  (as
shown in Figure 2-3) when resinous softwoods such as pine are
pulped.  Generally, the digester relief gases are vented to a
condenser to reduce the gas moisture.content and to a cyclone
separator to remove any small wood chips or fines.  The
                              2-16
-------
turpentine and water removed by the condenser are separated in
a decanter.  The turpentine, which is lighter than water,
overflows from the decanter to a storage tank.  The water
removed from the decanter bottom overflow is combined with
other process condensates for treatment.  During the decanting
process, HAP's are emitted through vents.  As shown in
Table 2-4 (emission point ID 16), raethanol is emitted from the
turpentine decanter at a level similar to that from a decker
or screen.
     Tall oil can also be recovered from the kraft pulping
process.  Tall oils are also found in resinous softwoods and
are recovered from the evaporation process using a tall oil
reactor, as shown in Figure 2-3.  Significant HAP emissions
are not expected from this step because it occurs after the
weak black liquor has been stripped of volatiles in the
evaporation process.  Table 2-4 provides emission factors for
this point (emission point ID 13).
     2.2.1.1.7  Condensate steam stripping.  Condensates from
the digester and evaporator, as well as from turpentine
recovery, are often combined and steam-stripped to remove VOC
from the waste streams and to reduce odors.  The VOC-laden
steam is then typically sent to an existing combustion device,
such as the power boiler, to take advantage of the heat
content and to destroy the VOC.  Table 2-3 provides vent
characteristics for condensate steam stripping (emission point
ID 11).  Emission factor data for the condensate stripper vent
are not available at this time.
     2.2.1.2  The Sulfite Process.  Figure 2-4 presents a
typical sulfite process diagram.  The sulfite process follows
the same basic steps as the kraft system with the exception of
coproduct recovery, which is not typically practiced in the
sulfite pulping process.  As in the kraft process, wood chips
are transferred to a continuous or batch digester and cooked
with cooking liquor.  However,  the sulfite process chemically
pulps wood using sulfur dioxide absorbed in an acidic
solution.  Typical bases include calcium, magnesium, ammonium,
                             2-17
-------
                                         VillBZZL
                           Is
                           SS
                                      IS
                                      II
                                      o S
                                                0)

                                                O
                                                O
                                                0)
                                               cc

                                               "S
                                                u

                                                £
                                              .  
-------
or sodium.  As shown in Figure 2-4, after digestion, oversize
particles are removed in the deknotting process and the pulp
is washed to remove the spent chemicals, screened to remove
oversize particles, and thickened to remove excess water.  The
chemicals removed in the washing process may then be recovered
for reuse.
     Spent cooking liquor removed from the washing process may
be collected and recovered.  In addition, chemicals can be
recovered from gaseous streams (i.e., red stock washers).  The
cost of all the soluble bases (with the exception of calcium)
makes chemical recovery economically feasible, which is also
attractive because of the pollution control achieved.
Chemical recovery is not practiced with the calcium-based
sulfite process because recovery is not cost-effective.
     The general steps of sulfite chemical recovery vary with
the type of base being recovered.  However, the process begins
with evaporation, as discussed in Section 2.2.1.1.5.  Because
this BID only focuses on process operation points, the sulfite
recovery process is not discussed in further detail.
Appendix C includes HAP emission factors and vent and
wastewater stream characteristics for the sulfite process. For
a description of the deknotting and washing processes, refer
to Sections 2.2.1.1.2 and 2.2.1.1.3.
     2.2.1.3  The Semi-Chemical Process.  The semi-chemical
pulping process is a combination of the chemical pulping
process and the mechanical pulping process and was developed
to produce high-yield chemical pulps.14  Figure 2-5 presents
a typical semi-chemical process.   The semi-chemical process
follows steps similar to the kraft or sulfite processes
discussed in Sections 2.2.1.1 and 2.2.1.2, namely, digestion
and washing.
     In the semi-chemical process,  wood chips are partially
digested with cooking chemicals to weaken the bonds between
the lignin and the wood.  Oversize particles are removed from
the softened wood chips, then the chips are mechanically
reduced to pulp by grinding them in a refiner, as in the
                             2-19
-------
                                                                            U8U8ZZZ.
                   2
                   M

                   O
ir
                                                   s-g

                                                    S
                                                   s?
                                                   S.5
                                11

                                II
                                i!
                                ,23
                 i!
           1
                                                       i
                                                       UJ
                                                       (9
£  E   §
«  S   2

I  5  5
I  I  "I
CO
CO

u
o

flu

O)
c

'a.


a.

15
o


-------
mechanical pulping process.  The pulp is then sent to storage.
Based on a voluntary industry survey, there are no semi-
chemical mills that practice chemical recovery.  However, some
mills combine spent liquor from on-site semi-chemical process
with spent liquor from an adjacent kraft process for chemical
recovery.
     There are two main types of semi-chemical pulping:
neutral sulfite semi-chemical (NSSC) and neutral sulfite
chemimechanical (NSCM).   The most common semi-chemical"process
is the NSSC process.15
     The only major difference between semi-chemical and
kraft/sulfite pulping processes is that the semi-chemical
digestion process is shorter and only partially delignifies
wood chips.  As with the kraft/sulfite pulping processes, HAP
emission rates from the semi-chemical process are dependent on
pulp production, wood type, and the chemicals used to weaken
the bonds in the wood.   Appendix C includes HAP emission
factors and vent and wastewater stream characteristics for the
semi-chemical process.
     2.2.1.4  The Soda Process.   The soda pulping process is
essentially identical to the kraft pulping process, except
that the chemicals used in the cooking process are
predominantly sodium hydroxide.   A small amount of sodium
sulfide is added to the sodium hydroxide to maintain greater
pulp strength and yield.16  Kraft digestion and washing
processes are discussed in Sections 2.2.1.1.1 and 2.2.1.1.3,
respectively.  Chemicals removed in the washing process are
collected and recovered.  Similar to the kraft process, the
soda chemical recovery process begins with evaporation, as
discussed in Section 2.2.1.1.5.   As previously discussed, this
BID only focuses on process operation points; therefore,  the
soda recovery process is not discussed in further detail.
     Data for vent and stream characteristics and emission
factors for the soda process are not available.  Because
little sulfur is added in the cooking liquor, sulfur compound
                             2-21
-------
emissions will be small.  However, organic emissions will be
similar to those from the kraft process.
2.2.2  The Bleaching Process
     The purpose of the bleaching process is to enhance the
physical and optical qualities (whiteness and brightness) of
the pulp.  Two approaches are used in the chemical bleaching
of pulps.  One approach, called brightening, uses selective
chemicals, such as hydrogen peroxide, that destroy
chromatographic groups but do not materially attack the
lignin.  Brightening produces a product with a temporary
brightness (such as newspaper).  The other approach -(true
bleaching) seeks to almost totally remove residual lignin by
adding oxidizing chemicals to the pulp in varying combinations
of sequences, depending on the end use of the product.  To
produce a high-quality, stable paper pulp (such as for bond
paper), bleaching methods that delignify the pulp must be
used.
     The most common bleaching and brightening agents are
chlorine, chlorine dioxide, hydrogen peroxide, oxygen, caustic
(sodium hydroxide), and sodium hypochlorite.17  Two less
common compounds presently used in the industry are ozone and
hydrosulfite.  Concern over chlorinated compounds such as
dioxins, furans, and chloroform have prompted the pulp and
paper industry to shift away from the application of chlorine
and hypochlorite and toward the use of other bleaching
chemicals such as chlorine dioxide in the bleaching process.
Table 2-5 provides a summary of the basic functions of each of
these bleaching chemicals.
     Typically, the pulp is treated with each chemical in a
separate stage, as shown in Figure 2-6.  Each stage includes a
tower, where the bleaching occurs; a washer, which removes
bleaching chemicals and dissolved lignins from the pulp prior
to entering the next stage; and a seal tank, which collects
the washer effluent to be used as wash water in other stages
or to be sewered.  Bleaching processes use various
combinations of chemical stages called bleaching sequences.
                              2-22
-------
      TABLE  2-5.
 COMPARISON OF COMMON CHEMICALS USED IN
             PULP BLEACHING
   Bleaching
   compounds
Bleaching
notation
Function
Chlorine

Caustic
(sodium
hydroxide)

Hypochlorite

Chlorine
dioxide
Oxygen

Hydrogen
peroxide

Ozone

Hydrosulfite
    C      Oxidize and chlorinate lignin.

    E      Hydrolyze chlorolignin and
           solubilize lignin.
    H      Oxidize and solubilize lignin.

    D      Oxidize and solubilize lignin.
           In amounts with Cl2 protects
           against degradation of pulp.

    O      Oxidize and solubilize lignin.

    P      Oxidize and solubilize lignin in
           chemical and high-yield pulps.

    Z      Oxidize and solubilize lignin.

 S or Y    Reduce and decolorize lignin in
           high-yield pulps.
                            2-23
-------
Bleaching
Chemical*
                                                 Vent to Scrubber
                                                  or Atmosphere
                                   Bleach Tower Plant

                                  Pulp/Chemical Slurry
                                                                                  Vent to Scrubber
                                                                                  or Atmosphere
                                                                  Recycled from
                                                                 Next We* Stage
                                                            Pulp and
                                                         Spent Chemicals
                                                                                   Vent to Scrubber
                                                       Seal Tank
                                                                    Recycle to Previous Wash Stage
                                                                             or Sewer
                                 LEGEND
                      O
     Point of Possible HAP Release
     (Source Identification)
"™~  Process Stream
- - Vent Stream
	  Liquid Stream
                                                                                                 I
                 Figure 2-6.  Typical Down-flow Bleach Tower and  Washer

                                                 2-24
-------
Table 2-6 presents the most common sequences used in kraft
bleaching.
     Sections 2.2.2.1 through 2.2.2.6 present information on
typical bleach stages.  Tables 2-7 and 2-8 provide the typical
vent and wastewater stream characteristics for bleaching kraft
pulps, and HAP emission factors, respectively.  Some of the
identified HAP's emitted by bleaching vents include chlorine,
chloroform, and methanol.  The wastewater from bleach plants
typically contains chloroform and methanol.  In most cases,
the emission factors presented in Table 2-8 are of the same
order of magnitude as those supplied by industry in June 1993
(NCASI technical bulletin 650) .
     2.2.2.1  Chlorination Stage (C-Stage).  The first stage
in the bleaching process is typically chlorination.  The
primary function of the chlorination stage is to further
delignify the pulp.18  The pulp is generally pumped into a
tower or stage similar to the one shown in Figure 2-6.  During
this process, chlorine reacts with lignin to form compounds
that are water-soluble or soluble in an alkaline medium, which
aids in delignifying the pulp before it proceeds to the next
bleaching stage or stages.18
     During bleaching, side reactions produce chloroform,
phenol, chlorinated phenolics, and other chlorinated organics.
These byproduct emissions, as well as unreacted chlorine, may
be vented from the chlorination stage tower, the washer, and
the seal tank.  Tables 2-7 and 2-8 provide emissions data for
these points.
     2.2.2.2.  Extraction Stage (E-Stage).  The next stage
after chlorination is typically the extraction stage.  This
stage and the remaining stages serve to bleach and whiten the
delignified pulp.  The extraction stage removes the
chlorinated and oxidized lignin by solubilization in a caustic
solution.  After the extraction stage, the pulp is washed to
remove the excess chemicals and solubilized lignin.  The
largest amount of unwanted lignin is removed in these first
two stages (chlorination and extraction).17  A portion of the
                              2-25
-------
        TABLE 2-6.   MOST COMMON KRAFT BLEACH SEQUENCES*



                                   Number of mills with
        Bleach  sequences13              bleach sequence

             C-E-H                           4

            C-E-HE-D                         3

          C-EO-HE-H-DE                       3

           CD-E-D-E-D                        4

            CD-E-H-D                         3

          CD-E-HE-D-E-D                       3

             CD-EO-D                         9

            CD-EO-H-D                        3

            CD-EOP-D                         3

            DC-EOP-D                         4

            DCD-EOP-D                        6


a Bleaching sequences performed at three or more mills are
  listed.  Approximately 90 other sequences are used at one or
  two mills for each sequence.

k Key:    C    =    Chlorination
          E    =    Extraction
          D    =    Chlorine dioxide
          H    =    Hypochlorite
          O    =    Oxygen
          P    =    Peroxide
          CD   =    Chlorine dioxide substitution
          EO   =    Oxygen added to extraction stage
          EOF  =    Peroxide and oxygen added to extraction
                    stage
                              2-26
-------
    CQ
H
O
H
CM

H
"*** *e
a 4i in
O v*
4I.Q
U 4-»
.2 c ^
0 0
X U
^
X
1
_ —
o « 3.
li. « 0.
u
Ir-l
1- 0 ^
41 CO 1—
U sx
§.-•§

ID Q.Q
I ID <
U sx
lit
^ O vx

w
c
'i
§
m

i







s«,
IP* (J
09 U.
•2g
E w
UJ


S


S

«


>jT
S
o

o
o
-o

o
o
in


§






^



*>
m
CO
ID
1
U



^
I


.-SooO^^o-o,,, .
^^^-CMOOcJcJ^1" '


zzzzzzzzzzz •

OOOOOOOOO'OO <


J-CM^
KIOOMOOKIOOrOO^
ooooooooooo

oooooooooooo
oooooooooooo

oooooooooooo
oooooooooooo
ininininininininininmin


§00000000000
ooooo-oo-o-ooo

10
10
1
^
ia
"c "c "c "c
41 U4I 1-01 U0> U
£ — 41 f — • HI -C — ' 01 f — • vx
(ACOX(ACOX(/)COXt/)CO
C04IOI04IOC04IOC04II.
XM*'X»)4'XM4'Xia4'
a)o>o)o>o)O)Oia)oioiDiiA
COCOCOIOIOCOCOIDCOCOID-
Ul«fAIAMIA(AW(/)(AIA<<-
1111*11111 U
ouaiujujooozzz.*
41
ID

*5
CO
3
                                                                                          o
                                                                                          o
                                                                                          -o
                                                                                          o
                                                                                          in
                                                                                          o
                                                                                          o>
                                                                                           41
                                                                                           4-*
                                                                                           ID
                                                                                           41
                                                                                           ai
                                                                                           ID
                                                                                          41

                                                                                          I
                                                                                          ID
                                                                                          U
                                                                                                              •o

                                                                                                              •o

                                                                                                               ID


                                                                                                              1
                                                                                                              V
                                                                                                               (A
   8.
 U U 4J  4-»
 C 2    CO
 u o ta  4i
 L. _ .—  .e
 41 u. f
H-    4-»  Of
 41       J=
OC  • U  4J
   00 ID
 e       a>

      «-
 ID >4- CO  C
   41 >  O
 M ae co  u

••" C 4^  4rf
 4-> S O  ID

'o p z  £
 5 5 u
 Q. ia    at
  z  »-
                                                                    2-27
-------








OS
o
PM
CO
(6
I
fe

25
o .,
LJ U3
CO "
_T ^J
Cu ^^
2< H

H
M "
^•1
o U
05 §
2 g
O „
a K


j W
o n
H E.
pi, EH
8§
fr ^



>4

S

g
CO




•
CO
(M

H
EH


































<",

CO
s
4"1 Q.
u
fl) 0)

§1
-
in -*
CM -O
d d

•* CM
in » o
i i •
o o o
XX «-
o
• in CM o
in r^ o



•O
CM CM
ro o
O 0
i i
N» «••
o o
O 0


fO
CM «O
1*1 (M
O •
i 0
^i '
03 m
o •-
o o
o o









c
ID
(_
-5 %
01 O
(A 4-*
01 01
OI OI
a ca
IA IA

u uj














CO O
° 0

O 0
1/1 ^*b
fO (M
s §
O 0




01
IA ID
10 01
2 (0
01 01
oi oi
ID ID
IA IA
i i
UJ UJ











CM
O
o
o ro
0 §
t^- d
0 i
o «-
o o
o o
o o
0 0




0 O
0 O




IM CM
o o
o d
I 1
§o
o
o
o
0 0



O Or
d °.
§* 1

o
o
0 0
0 0


•o
s ^
d °-



o o
o o











01 J=
1 IA
O ID
<-> 2
01 01
O) OI
ID ID
in IA

o o













IM r*i
d •
i O
§ £
§ S
§ §
0 0




i ..
0 0
0 0




i
o
> in
s °.
§ ?
O vT
0 0
O 0



° »
o •-
>o d
O i

i i
0 O


CM
O CM

a a
IA IA
i i
O 3=

















•- CO
0 0
0 0




ro
o
5 §
0 0







ro
S §
0 0








«- 0
0 0







«~ o
0 0









-g
ID

'w To
S SI
01 01
OI OI
a a
IA IA

3B X
















"I
O
0
0





o




in
8

d
o




ro
LA
O
i
™
0


CM
in



«—
o


01
OI
ID
IA

^

^
ID
a"
CJ
u
oi 2
IA ID
•o fc
w **
U —




C_
01
+4

0)
**
co
3






M
O
0
d





o




ro
CM
8

o
CM
O
o
o
d




CM
^

i
S
d


CM
ro
d



O
d






V
01
a
i
u
01
3
a>
0?
.its
** (.
S-
CO M-















§ ;
w

'=
OJ
0)
^
o
X
4-*
—
I
L.
CO
,j
C
01
(0
01
^ •
a co
01 U.
1- O
CA O

2 0
01 CA
IA IA
01 '~

h^ C5
,j
CO >
.2 "2
•0 CO
oi a.
& z


•S §
g i
en • C
««
M °
in w


w* •*
§ ..E **
"s §
01 > T3
j: — - oi
W OI IA
S
?s
(0 CO C.
— CO
ai a.
IA IA
0> i^ ^
£| 4 S
l!e 1."

£ ** 5 o c .2
° -= 2 « » 3 »
^J ^ iW *^ t ""^ V)
H— o t» o o S
O £ U UJ CJ =B o

W »^ " " " "
.2 g 01 4. 0* «• ?
c M OI O) oi OI m
y in co co a co
o a ca CA CA co <
— CA ' ' ' ' Z
^ L. u uj a x
•i* O -^
o w •• a
S-5 s 2


to .a u
2-28
-------
filtrate from these stages may be reused and the remaining
filtrate sewered to prevent precipitation of the solubilized
chlorolignin compounds.19  Emission factors for total HAP,
chloroform, methanol, and chlorine released from the
extraction stage tower, washer, and seal tank are shown in
Table 2-8.
     2.2.2.3  Chlorine Dioxide Stage fD-Stage) and
Substitution Stage fC/D-Staqe).  Chlorine dioxide is often
used in bleaching, either in the chlorination stage (as a
substitute for some of the chlorine usage - chlorine dioxide
substitution) or as an additional chlorine dioxide stage.  The
chlorine dioxide stage is similar to the chlorination stage
and has similar emission points.  Chlorine dioxide has
2.63 times greater oxidizing power (on a pound-per-pound
basis) than chlorine and is used for nearly all high-
brightness pulps.2 °
     Chlorine dioxide has a high selectivity in destroying
lignin without degradation of cellulose or hemicellulose.
When chorine dioxide is added before chlorine less chlorinated
organics are released into the effluent.  Consequently, using
the additional chlorine dioxide step has improved the
delignification of the pulp and effluent characteristics.21
     Chlorine dioxide is typically generated on site as a gas
from the reaction of sodium chlorate in an acidic
solution.22   Tables 2-7 and 2-8 provide vent and wastewater
stream characteristics and emission factor data for the
chlorine dioxide stage components.
     2.2.2.4  Hypochlorite Stage (H-Staqe).   Another common
bleaching stage is hypochlorite.  Hypochlorite is a true
bleaching agent that destroys certain chromophoric groups of
lignin; however, it also attacks the cellulose to some extent.
High cellulose degradation occurs in kraft pulp,  so the
application of hypochlorite to kraft pulp is usually used only
as an intermediate stage of the sequence or to produce semi-
bleached pulps.   Hypochlorite can also be used as an effective
bleaching agent for sulfite pulps.  However, the hypochlorite
                             2-29
-------
stage has been identified as one of the most significant
points of chloroform emissions.23  studies conducted by
NCASI show that bleaching sequences without hypochlorite have
lower chloroform emissions.23 .Vent and wastewater.stream
characteristics and HAP emission factors for the hypochlorite
stage are given in Tables 2-7 and 2-8, respectively.
     2.2.2.5  Ozone Bleaching Stage (Z-Stage).   Ozone
bleaching is effective for further delignification as well as
bleaching and brightening.  Ozone bleaching does not result in
the formation or emission of chlorinated organic compounds
such as chloroform.24  Currently there is only one full-
scale ozone bleaching line operating in the United States, and
HAP emissions from this process have not been measured.
     2.2.2.6  Peroxide Stage (P-Stage).  Another potential
bleaching stage is the peroxide stage.  Peroxides, generally
hydrogen peroxide, are effective lignin-preserving bleaching
agents.  Peroxides are frequently used as bleaching agents in
the first extraction stage or in later stages of the bleaching
process.  Peroxides increase brightness without significant
losses in the yield strength of highly lignified pulps and
generate fewer chlorinated organic emissions.   Emissions from
this stage have not been measured.
2.3  BASELINE EMISSIONS
     This section presents national baseline emission
estimates for the process operation points in the pulp and
paper industry.  These emission estimates were developed based
on the uncontrolled emission factors presented in this
chapter, adjusted to account for the baseline level of control
in place on these points.  Baseline control levels were
determined through a review of applicable State and Federal
regulations and from information provided by many facilities
regarding their current level of control.  Sections 2.3.1 and
2.3.2 summarize Federal and State regulations, respectively,
for the pulp and paper industry.  Section 2.3.3 summarizes
baseline controls assumed to be in place because of these
                              2-30
-------
regulations.  Section 2.3.4 presents national estimates of
baseline emissions.
2.3.1  Summary of Federal Regulations
     The EPA has developed new source performance standards
(NSPS) for kraft pulp mills.25  The NSPS established two
emission limits for TRS compounds from points that include
digester systems, multiple-effect evaporator systems,
brownstock washers, and condensate strippers.  Table 2-9
summarizes the Federal regulations for these process operation
emission points and provides the maximum emission rates on a
concentration basis.
     Although these regulations do not specifically address
HAP's from the pulping process, facilities with new processes
affected by this rule are achieving the required TRS limits
through the collection and combustion of vent gases, and are
thereby reducing organic HAP emissions from these vents by at
least 98 percent.
2.3.2  Summary of State Regulations
     In addition to the NSPS, which applies to new and
modified sources, many States have adopted similar limits for
existing sources.  State regulations pertaining specifically
to process operation emission points are summarized in
Table 2-10.  Over 60 percent of the facilities in the United
States are in States with current pulp and paper regulations.
In determining baseline levels of control, it was assumed that
facilities in States with TRS emission limits on digester
systems, evaporators, brownstock washers, and condensate
strippers are" controlling these points through combustion, and
facilities in States with bleach plant chlorine and chlorine
dioxide limits are scrubbing the vents from these stages.
Industry has commented that some States reported in Table 2-10
may have additional control.  This information was used as a
secondary determination of control if no information was
provided through industry survey responses.26
     ITT addition to the regulations summarized in Table 2-10,
North Carolina,  Tennessee, Maryland,  and Michigan have passed
                             2-31
-------
    TABLE 2-9.
             SUMMARY OP FEDERAL REGULATIONS (NSPS) FOR
              EMISSIONS FROM KRAFT PULPING FACILITIES3
    Process unit
                    Emission limits*5
 Method of control
 Kraft digester
 system
 Kraft brownstock
 washer system
                   5 ppm  of TRSC
                   5 ppm of TRSc/d
 Multiple-effect      5 ppm of TRSC
 evaporator system
 Condensate stripper  5  ppm  of TRSyc
 system
 New,  modified,  or    5  ppm  of  TRSC
 reconstructed kraft
 digester system
Lime kiln, recovery
furnace, or
combustion at a
minimum of 1200 °F
for 0.5 sec

Lime kiln, recovery
furnace, or
combustion at a
minimum of 1200 °F
for 0.5 sec

Lime kiln, recovery
furnace, or
combustion at a
minimum of 1200 °F
for 0.5 sec

Lime kiln, recovery
furnace, or
combustion at a
minimum of 1200 °F
for 0.5 sec

Lime kiln, recovery
furnace, or
combustion at a
minimum of 1200 °F
for 0.5 sec
a
b
c
d
New Source Performance Standards, 40 CFR 60, Subpart BB.
Key:   TRS  =    Total Reduced Sulfur
       ppm  =    parts per million (by volume, dry basis)

Corrected to 10 percent oxygen.
Standard does not apply to facilities where implementation
has been demonstrated to be technically or economically
unfeasible.
                             2-32
-------
rH
0
Ui
-p
c
o


•H
«J
2
jyi
0)
Ul
Ul
0)
-P
CO

m
Ul
4J
•H
e
•H
rH

C.
O
-H
Ul
Ul
•H
U






4J
•H
C
3

CO
Ul
Q)
o
o
Ui
ft









TJ
C (U C
O-H O
C -H 4H -H
O -P -H 4J
•H (0 O (0
•P Ul (U Ul
Ul O ft 0)
3 C Ul C
XI -H -H
e o -P u
o c o c
u H a H



3
h-l
%.
CO
s

_ ?
fa U

> O H
w" o" a J
a CO H <
ft
Q


c
o
CO -P
OS ^>
EH W
OS
4-1 EH
O
X!
ft ""*
ft CM
*
in rH






J^
i
« w





'O T3
0) (U
•H -H
(II Mj
•H -H
0 0
QJ 0)
ft ft
Ul Ul
4-> 4->
O O













Q i"*J
aft
ft
Q


C
O CO
•P OS
^~- EH
CO
OH *W
EH 0

pQ r3
ft
VO
• O
o CM



Ul
1 O
Q) 4J
to rH nj
(!) ft Ui
•P -H O
Ul -P ft
0) rH (0
C71 3 ?>
•H g 0)
TJ "••»
g -P
4J 0) O
4-i -P o)
«j w  Ul 0) (U
Ul 0) ft G
3 C Ul W
XI -H
6 O -P -P
O C O 0
cj H a a





<
u

*? *? '
o 5

w u a
a w EH
rtj" i-}" C0~ J
> fa a <
ft
Q
•^

C
o
CO -P
OS "•»-
EH CO
OS

3 0)
g

-P O
4H <0
(0  u co






CO
os
EH
4-1
O
ft
ft

m




0)

(0
CO
C
0)
T3
C
O Ui
U 0)
ft
4J ft
fl^ i ,-J
*F"1 r^
(0 Ui
Ul 4->
M 01





TJ TJ Tf TJ
O 0) 0) Q)
•H >H -H -H
-H -H -H -H
O 0 0 0
Q) 0) (U 0)
ft ft ft Q.
Ul Ul 01 Ul
4J 4J -P 4J
O O O O













W < W <
a o a o


CM
rH CM
CMCJ O CN
rH rH O
O 4-1 U rH
0 U
O Ul O 4-1
ft 0
Ui -^ Ul
.CXt £ XJ
xT1"1 xf"1
•H CM rH rH
• •
O O ft O








4-1
C
m
rH
ft

x;
o
m

•H
CQ






c
o
•H
4J
(0
Ui
(U
c
•H
o
c
H












J
fa
^
•H
o

c
0
4->
^»,
CO
EH

XI
rH
in
•
o






4J
C
ti
rH
ft

rH
•H
O

rH
rH
(0
EH





•O'
0)
•H
•H
CJ
(1)
a
4->
o













ffi
a
ft
Q
<;

C
O

1 — ,
CO
'En

s
H
•
Q\







01
rH
rH
•H
g

0)
.p
•H
4-1
rH
3
W





TJ
0)
•H
•H
O
ft
01
^J
0
a












^
S








CO
c\
33

ft
ft

o
in






Ul
TJ

O
ft

4J
C
0)
3
rH
4-1
(ii
Dc3








0) o
TJ TJ
X 4-1
O rH
•J H
~ ^
73 W
(DOC
C C 0)
•H «H ^
Ul Ul O
O O Ul
rH rH TJ
X! J3 >t
U O S


II II II

CM
CMO CO
rH rH CM
0 U X


•
Ul
3
4H
rH C
3 O
CO -H
rH ft
TJ rH rH
(U -H 3
U g ft
3
T3 Ul TJ
0) 0) 0)
OS ft-H
Ui
rH CO Q
fO 4-J 1
4-> Ui Ul
O (0 -H
EH ft<
ol
H
II II II
>t
Ul
CO E ft (0
OS ftO 3
EH ft< C
(0
hj

Ul
.. Q)
^M jl
r^ T—
(U (M
^ (4?

(0 Xt
2-33
-------
regulations that limit toxic air pollutant emissions.  These
regulations limit the maximum ambient air concentrations of
toxic air pollutants surrounding the pulping facilities, as
determined by dispersion modeling.  Although these regulations
do not specifically limit HAP emissions from the pulping
process, to compliance with these ambient air concentration
limits achieves some HAP emission reduction.  Some of the
additional "controls reported by facilities and incorporated
into the baseline control evaluation were likely put" into
place to comply with these toxic air pollutant regulations.
2.3.3 Baseline Emission Controls
     Summaries of existing control techniques used for pulping
and bleaching vent points are presented in Tables 2-11 and
2-12, respectively.  As shown in Table 2-11, emissions from
nearly all kraft and sulfite digester blow and relief gases
are being controlled, as are those from some of the semi-
chemical digesters.  In addition, turpentine decanter vents,
evaporator noncondensibles, and evaporator hotwell vents are
being controlled at most kraft and some sulfite mills.  Much
smaller percentages of washers, deckers, and knotters at kraft
mills are being controlled.  However, washers are being
controlled at almost half of all sulfite mills.  As shown in
Table 2-12, scrubbing of bleach plant vents ranges from
approximately 30 percent of individual extraction stage vents
to approximately 90 percent of first stage chlorine dioxide
vents.  Combustion devices and gas absorbers (scrubbers) are
discussed in Chapter 3.0.
     Table 2-13 summarizes the extent to which wastewater from
pulping unit processes is pretreated prior to discharge to the
wastewater treatment system.  Condensates from approximately
25 percent of kraft mill turpentine recovery units and
evaporator systems are pretreated with air or steam stripping.
A smaller percentage of the digester blow tank condensates in
kraft, sulfite, and semi-chemical mills are pretreated as
well.  Steam strippers and air strippers are discussed in
Chapter 3.0.
                              2-34
-------
TABLE 2-11.  SUMMARY OF EXISTING TECHNIQUES TO CONTROL HAP
                 EMISSIONS FROM PULPING VENT SOURCES*
Vent emission source
Batch relief gas
Continuous relief gas
Batch blow gas
Continuous blow gas
Turpentine decanter
vent
Evaporator (hotwell
noncondensibles)
Washer screens
Washer filtrate tanks
Washer hood vent
Deckers
Knotters
Percent
Kraft
97
95
91
88
73
88
5
11
6
9
8
controlled in industry*3
Sulfite
100
0
92
0
0
55
0
57
38
0
0
Semi-
chemical
0
33
0
25
NAC
NAC
0
0
- 0
0
NAC
a Data taken from Reference 3 .
b Sources are assumed to be controlled with at least
   98 percent destruction efficiency for VOC and organic
   HAP.
   For this analysis, only one semi-chemical mill was
   known to practice chemical recovery and none were
   known to practice turpentine recovery or bleaching.
                           2-35
-------
   TABLE  2.   SUMMARY OF  EXISTING TECHNIQUES  TO CONTROL  HAP
                EMISSIONS FROM BLEACH VENT SOURCES
     Stage
 Emission
  points
controlled
                               Bleach lines
                               controlling
                               at baseline3
  Assumed
  Control
efficiency13
Chlorination
First
extraction
Hypochlorite
First
chlorine
dioxide
Second
extraction
Second
chlorine
dioxide
Tower
Washer
Seal tank
Tower
Washer
Seal tank
Tower
Washer
Seal tank
Tower
Washer
Seal tank
Tower
Washer
Seal tank
Tower
Washer
Seal tank
69
69
62
28
34
51
18
26
41
95
79
92
32
41
59
76
57
76
99% Cl and HC1
99% Cl and HC1 -
99% Cl and HCl
99% Cl and HCl
99% Cl and HCl
99% Cl and HCl
a Percent controlled at baseline for individual bleach stages.
  However, when the level of control is evaluated on a
  sequence basis, 15 percent of facilities have all equipment
  controlled.
b Control applied is a scrubber.
                              2-36
-------
    TABLE 2-13.
SUMMARY OF ADD-ON CONTROL STATUS OF
   WASTEWATER EMISSION SOURCES3
Wastewater emission source
Digester blow condensates
Turpentine decanter underflow
"Foul" evaporator condensates
"Clean" evaporator condensates
Bleach plant wastewater
Percent
Kraft
12
22
26
0
0
of unit processes
controlled
Sulfite
3
0
0
0
0
Semi-
Chemical
3
NAb
NAb
NAb
NAb
Data taken from References 1 and 3.
For this analysis, only one semi-chemical mill was known tc
practice chemical recovery and none were known to practice
turpentine recovery or bleaching.
                          2-37
-------
2.3.4 Baseline Emissions
   Baseline emissions are essentially uncontrolled emissions
adjusted for the effects of current State and Federal
regulations, as well as additional controls known to be
currently in place.  Estimated baseline emissions from process
operation points in the pulp and paper industry are summarized
in Table 2-14.  Estimates for baseline emissions of total HAP,
total VOC, TRS, and 15 major HAP and VOC contributors are
presented in Table 2-14.  As shown in the table, methanol is
the largest constituent contributing to total HAP and total
VOC emissions for the included emission points.
   Descriptions of the process used to estimate including
national emissions using estimation process, the models and
database developed for this purpose are given in Chapter 4.0
and Chapter 6.0, respectively.  The estimated baseline
emissions are based on emission factors (Appendix C), mill-
specific data  (e.g., pulp/bleach production), Federal/State
regulations (Tables 2-11 and 2-12), and capture efficiency and
emission reduction efficiency of the control devices
(Chapter 3.0).
                              2-38
-------
 TABLE 2-14.   SUMMARY OP ESTIMATED NATIONAL BASELINE EMISSIONS
                      PROM CHEMICAL AND SEMI-CHEMICAL
                      PULPING AND BLEACHING OPERATIONS3
           Major Pollutants
Emissions (Mg/yr)
         Total HAP
         Total VOC
         Total reduced sulfur
         Methanol
         Hexane
         Toluene
         Methyl ethyl ketone
         Chloroform
         Chlorine
         Formaldehyde
         Acetaldehyde
         Methylene chloride
         Propionaldehyde
         Acrolein
         Acetophenone
         Hydrochloric acid
         Methyl chloroform
         Carbon disulfide
       170,000
       830,000
       350,000
       120,000
        18,000
        14,000
         6,000
         3,300
         2,800
         2,100
         2,00(T
         1,200
           700
           700
            60
            59
            22
             8
a  Based on process operation emission points only (chemical
   recovery sources other than evaporation are not included).
                             2-39
-------
2.4  REFERENCES

1.    Responses to the 1990 U.S. EPA National Census of Pulp,
     Paper, and Paperboard Manufacturing Facilities Section
     308 Questionnaire and supplements (Confidential Business
     Information).  1992.

2.    Memorandum from Wendy Rovansek, Radian Corporation, to
     Pulp and Paper Project Team.  Pulp and Paper Mill
     Math II.  June 29,  1993.

3.    1991 Lockwood-Post's Directory of the Pulp, Paper, and
     Allied Trades.  San Francisco, Miller Freeman
     Publications.  1990.  p. 9.

4.    Smook, G.A.  Handbook for Pulp & Paper Technologists.
     Atlanta, GA, TAPPI and Montreal, Quebec, Canada, Canadian
     Pulp and Paper Association.  1987.  p. 39.

5.    Ref. 4, p. 2.

6.    Memorandum from Greene, D.B.  Radian Corporation, to
     Shedd, S.A., EPA/CPB.  Heat Release Factors.
     September 30, 1993.

7.    Environmental Pollution Control, Pulp and Paper Industry,
     Part I, Air.  U. s.  Environmental Protection Agency,
     Technology Transfer.  Publication No. EPA-625/7-76-001.
     October 1976.  p. 1-4, and  pp. 2-10 through 2-11.

8.    Ref. 5, p. 67.

9.    Ref. 5, p. 89.

10.  Ref. 5, p. 91.

11.  McDonald, R.G. and J.N. Franklin, eds.  Pulp and Paper
     Manufacture:  The Pulping of Wood.  Second Edition.
     Volume 1.  New York, McGraw-Hill Book Company.  1969.
     p. 486.

12.  Ref. 5, p. 164.

13.  Ref. 5, p. 124.

14.  Casey, J. Pulp and Paper Chemistry and Chemical
     Technology.  Third Edition.  Volume II.  New York, John
     Wiley and Sons.  1980.

15.  Ref. 5, p. 40.

16.  Ref. 12, p. 350.                       --             _  . —
                              2-40
-------
17.  Ref. 5, p. 154.

IS.  Ref. 5, p. 160.

19.  Ref. 5, p. 170.

20.  Ref. 5, pp. 166 through 167.

21.  Liebergott, N., et al.  A comparison of the Order of
     Addition of Chlorine and Chlorine Dioxide in the
     Chlorination Stage.  TAPPI Journal.  October 1990.
     p. 207.

22.  Ref. 5, p. 158.

23.  Results of Field Measurements of Chloroform Formation and
     Release From Pulp Bleaching.  Technical Bulletin No. 558.
     New York, National Council of the Paper Industry for Air
     and Stream Improvement, Inc.  December 1988.  p. 2.

24.  Byrd, Medwich, V. Jr., et. al., "Delignification of
     Chemical Pulps with Ozone:  A Literature Review."  TAPPI
     Journal, March 1992.

25.  Code of Federal Regulations, Title 40, Part 60,
     Subpart 280.  Applicability and designation of affected
     facility.  Washington, DC.  U. S. Government Printing
     Office.  June 23, 1989.

26.  Responses to Industry Survey discussed in the following
     letter:   J.E. Pinkerton, National Council of the Paper
     Industry for Air and Stream Improvement, Incorporated
     (NCASI), to J. Telander, EPA: 15B, and P. Lassiter, EPA:
     CPB.  February 11, 1992.  (Responses were claimed
     confidential business Information).
                             2-41
-------
                3.0   EMISSION CONTROL TECHNIQUES

3.1  INTRODUCTION
     This chapter discusses demonstrated techniques that can
be applied to reduce HAP emissions from the pulping and
bleaching process points discussed in Chapter 2.0.  Control
devices are typically applied to an emission point vent or
wastewater stream to reduce HAP's in the vent gas or-
wastewater stream.  Details of these controls are presented in
Section 3.2 (vent controls) and Section 3.3 (wastewater
controls).  The techniques presented are candidates for
control options that may provide the basis for the emission
reduction requirements of the pulp NESHAP.  Industry has
commented that the methanol removal efficiencies for scrubbers
and steam strippers presented in this document are overstated.
However, the information provided in this chapter documents
the analyses to date, based on available data.  As the
industry provides data to support these comments, these data
will be considered.
     Process modifications and substitutions affect the
formation of HAP compounds in pulping and bleaching processes
by changing the emission point or by altering the process
operating conditions or process chemicals used.1  Table 3-1
presents a summary of the process modifications and process
substitutions under consideration as candidate control
techniques.
     The pulping process modifications (extended cooking,
oxygen delignification, and improved washing)  reduce the
quantity of lignin in the pulp going to the bleach plant,
thereby potentially reducing the quantity of chlorinated
organics.formed.  Appendix C includes emission factors for
                              3-1
-------
           TABLE 3-1.  PULPING PROCESS MODIFICATIONS  :
                       AND BLEACHING PROCESS SUBSTITUTIONS*
                 Pulping Process Modifications
                       Extended Cooking
     (modified continuous cook  [MCC] and rapid displacement
                        heating  [RDH])
                    Oxygen Delignification
                  Improved Brownstock Washing

                Bleaching Process Substitutions
                 Chlorine Dioxide Substitution
                  Elimination of Hypochlorite
               Oxygen/Peroxide Use in Extraction
                    Split Chlorine Addition
	Ozonation	
a  Reference 1.
                              3-2
-------
several of the process modifications and substitutions
discussed above.
     The bleach plant process modifications and substitutions
focus on reduced use of chlorine and hypochlorite to achieve a
reduction in chloroform generation.
3.2  APPLICABLE CONTROL TECHNIQUES FOR VENTS
     This section presents control devices that are applicable
for reducing HAP emissions from pulping and bleaching process
vents.  Many kraft facilities currently control some of their
pulping vents by ducting to a combustion device and some of
their bleaching vents by scrubbing.  Table 3-2 presents a
summary of the combustion devices currently being used to
control different pulping vents in kraft pulp mills.2  As
shown, the most commonly used combustion control devices are
lime kilns and power boilers, and most facilities currently
control their digester relief and blow gases, evaporator
noncondensibles and hotwells, and (where applicable)
turpentine decanter vents.
      Although less frequently controlled than vents, fugitive
sources such as knotters and washers are controlled by some
facilities.  Sulfite mills typically control their pulping and
bleaching vents by scrubbing.  Scrubbing of the pulping vents
is used to recover sulfur dioxide, which is used to generate
cooking liquor.  These scrubbers are also believed to remove
the majority of the methanol in the.vent streams.
     To determine a control strategy for the identified
pulping and bleaching emission points, those points that are
currently controlled were evaluated.   For pulping vents,
combustion devices were considered; for bleaching vents,
scrubbing alone, scrubbing and ducting the scrubber off gases
to a combustion device,  and incineration followed by scrubbing
were evaluated.  For pulping emission points that may be
currently hooded but not fully enclosed (i.e.,  fugitive points
such as knotters and rotary vacuum pulp washers), enclosure
followed by conveyance to a combustion device was evaluated.
Table 3-3 presents pulping emission point vent stream
                              3-3
-------



«f
CQ
W
O
H
Q

.4
O
gw

0
u

o
H
CQ
D
8
0
O
§
H
CO
D
CQ
J
H
s
fa
o

&^ "
55
H
CJ

W
Pi


•
(M
1
<*)

pa
j
n
rtj
g4



















a)
o
•H
0)
T3

C
O
,_j
^n
•P
Ul
3
X)
g
O
U








rH
trt
(U
-P
O
EH

j_i
O
-P
(0
0)
•H
o

H


r*1 Q)
0) °
^ *
8§
QJ (ii
Pi

t^
>H QJ
I-H
X



0) C
g rH
•H -H






Ul
0)
0

3
0
w

C
o
•H
Ul
Ul
•H
g












r-
en






r-
01








O





OJ




5






(0
(0
n^

til
Q)
•rH
rH


J^
o

(0
J_l
O
ft
(0
>
M


in ^ vo en co






o o o o o








o o o o o





O O vo vo If)




in JUj o n n
H
rH
(U
*J
-P
O


»
Ul
0) Ul
rH ^
XI C
•H flj
Ul 4J
C P
(1) Q) C
'O - Ul -P 
O 0) 5-1
O (U 4J "O
C M rH O
O O -H O
C W  J3 X! fi ^4 -P
• Ul Ul Ul O O
0) rtJ (0 flj 0) C
'*"' 12 2 S Q M































•
OJ

0)
O
C
0)
5-i
Q)
4H
0)
OH

g
O
5-i
<4H

C
fll
i_^
(0
•p

(0
•p
(0
Q


n)
3-4
-------







W
2
..
0
ft

2
0
CO
to
H
jg
ca

o .
H
^H
D
Q|

i
<^
g
O
PM


U
H
H
ca
H
-fcj
re
H .
b
p*
^Jj
9
03
f£
u


p<
S5
M
^
J
rt
o
H
ft
frH




ro
1
ro
H
n
rt
£4









2 o-o
g <*H a>
to h
T> T) C
5: 01 it
M 0) C
c



s —
0) c
1 1 E
C C

U ^
4J *

X


0) ,,
V4 "X
•*jj ^J 4P
o 8
23


J3
ftc?
so
0) ^.
EH





.Q 	
*£ id1
* °rH
rH '-' ?
C*4






0)
cn
c -~
id >i
u m
•o
4J EH
•39
id -~
ft
id
O







4J
C
a

c
0
"4
CO
m
"4
C
W






O
2










O
^






cn
1
o
n




O
0
t-H
1
tn
vo






ro
rH











O
o
CO
1
cn








tn
id
cn

1
rH

14
11)
4J
to
0)
D>

•o
U
4J
id
CQ



0


















o
1
tn
ro




O
tn
rH
in






vo
o
d











0
o
CO
i
cn







3
0

f}

14
01
4J
CO
0)
cn
•rt
•o
tn
3
O

C
e 01
Sid
cn



O
z








o
o

CO
rH





O
CN
1
m




O
tn
CN






vo
CN
o
o
d











o
0
CO
i
cn












tn
id
cn
IM
0)
-H
rH
0)

14
0)
01
0)
Cn
a



01
0)
^*









o
CN






O
i-H
1
CN




in
I
o
CN






cn
d











o
O
CO
1
en








^
^|
0
4J
id
^
•M«r

•o
I

^^
VI CO
0) C
4J 0)
4J 0)
0 U
c u
^4 01



01
0)
^^









o
•*






o
i-H
1
CN




in
1
o
CN






cn
d











tn
CN

7*
in





















0)
01 *
id



O
Z










0
CN






in
n
1
tn
rH




in
t-
in
in






co
rH
O











in
CN
vo
i
tn
vo






Q
id
0


•a
id
c
id
^)

id
0)
ca

0)
£ .*
01 C
id id
3 4J



01
0)
^j
^*









CN
d






o
rH
1
CN




in
I
o
CM






en
d











in
CN
vo
I
in
vo















C
0)
0)
u
m
••^
14
0)
U
0)
a



0








o
o
rn
rH
CN





o
cn
o
in




in
rH
I
o
co






c*
CN
O
o
d











m
CN
vo
I
m
vo












rH
rH
0)
3

0
A
^^
0
4-1
id
D
O
ft
id
U



0








o
o
co
CD
rH





0
(N
1
m




o
vo
in
CN






vo
CN
0
o
o











o
0
CO
1
«*•
cn











14
0)
CO
c
0)
•o
c
o
u
0)
c
*«H
4J
i

£

0)
>l 14
*O 4J
ft
«4J id >.
cn id o rH
X C
CO 0) 0
6 "4 4J
1 a) -a
o c ft id
vo id e
r- O 0)
^^ O W
•a ^r 3
C 14 4J
m ai o ft
o <*H id
u c u
o 0) T)
rH Ll 01 01
• 0) TJ 4J
i-H VW 0) 0)
CN 0) 0) rH
<- U C ft
01 CO 0
id g -H u
cn id
01 oi cn
>1 U 14 C
14 4J 3-4
Tf CO CO >
0 0)
 C U
to > 0) id
00) C 0)
• 4J 4J
>i-^4 * 0
Id TJ C — 4J
TJ C -4 0)
•*«. O > TJ
01 U 01 -^4 Q)
C TJ 4J S
O TJ C "43
4J U 3 Cn in
id o 3 m
4J TJ ft -i ja e — i
4J E
EH 0) TJ id 01
§14 0)
id co 0) oi
m s. J3
10 0) 4J 4-1
• Ql rH
ro 4J 01 0 •
Id 14 4J 01
0) 14 CO
O 4J C "4
c 3 id a) 3
0) 0 0) ft 14
14 rH £ 00)
0) b, £
MH 0) CO 4-1
01 JS -4 O
(X • 4J
CN • 4-> •» •
E to m c ai 0)
0 0) -4 C -4 O O
14 U O O C C
i >i
0) 14 0) -H C 0) 0)
14 Q) 4J TJ 0 > >
id HH C C -4 C C
0) 0 O CO O O
ca « o o to o o
0) -H
"4 C 4J TJ S 0 CO
4-> 0 Id H 0) 4J 0)
-4 0) id 14
0 TJ JSTJ C >W-r(
id 01 C id 0 3
ft a ai id -4 o*
id id jC 4-> VM )-i oi
tj n EH n M ft M

id a o TJ
3-5
-------
characteristics and identifies which points needed enclosures
prior to routing to a combustion device.2/3/4  The emission
point characteristics presented in this table should be
considered in selecting an appropriate control device.
Section 3.2.1 discusses the vent gas collection and transport
system that is used to capture and convey vent gas to a
control device.  Section 3.2.2 discusses applicable control
devices for pulping and bleaching vent streams.
3.2.1  Vent Gas Collection and Transport System
     To control HAP emissions from pulping and bleaching
operations using stand-alone or existing devices, vent streams
must be captured and transported to the control device.
Additionally, the vent gas may be conditioned in the transport
system to alter its characteristics before it reaches the
control device.
     Typical components of the capture and conveyance system
are the hoods or enclosures, pipe or ductwork, the prime mover
employed (i.e., fan), gas conditioning equipment (if needed),
and safety devices.
     Two methods are generally used to capture vent streams:
(1) hard-piping and (2) hoods or enclosures.  The method used
depends on the emission point type and will affect the
volumetric flow rate and relative organic compound
concentration of the vent stream.  When an emission point is
an enclosed process with a vent, the vent can be hard-piped to
a control device, thereby reducing the introduction of ambient
air into the vent stream, and reducing the vent stream flow
rate.  Digester gases and evaporator vent gases are examples
of vent points that can be hard-piped to a control device.
     When an emission point is diffuse or large, such as a
washer or decker, vent emissions may be captured using an
enclosure or well-enclosed hood and then hard-piped to a
control device.  Hood collection efficiency is a function of
capture velocity, which depends on the creation of an air flow
                              3-6
-------
that is sufficient to capture the contaminated air emitted
.from the point and draw the air into the exhaust hood.5  At a
constant volumetric air flow rate, hood capture efficiency
decreases as the distance between the point and the hood
increases.6  Based on discussions with vendors, enclosures
can be constructed to achieve complete capture.  A 34-percent
reduction in flow was assumed when replacinga hood with an
enclosure for pulping vent streams.7
     The type of duct material used is determined by the
characteristics of the gas in the vent stream.  Two materials
commonly used for ducts in the pulp industry are fiberglass
and stainless steel.  Fiberglass ducts have the advantages of
relatively low cost, light weight, and corrosion resistance.
Fiberglass is commonly used for venting bleach plant towers
and washer hoods.  The problems identified with using
fiberglass ducting in the pulp industry are its inability to
be electrically grounded to prevent the buildup of static
charge and the absorption of hydrocarbons in its fiberglass
resin.
     Stainless steel is the preferred material of construction
for non-condensible gas (NCG) transport systems.8  Although
it resists corrosion by water and sulfur compounds, stainless
steel is susceptible to corrosion by chlorides and is,
therefore, not used for conveying bleach plant vent gas
streams.9
     Ductwork may be insulated to reduce the amount of vent
gas cooling that takes place in the ducting and to prevent
freezing of moisture in the duct during winter.
     Vent streams in the pulp industry, such as those from
digester blow gas vents, may have sufficient pressure to
convey the vent gases through the transport system to the
control device.  When insufficient pressure is provided by an
emission point, or where the source of emissions has to be
captured (such as pulp washer hood vents), fans must be used
to convey the vent gases.   However, fans may not be the most
desirable prime movers in transport systems conveying
                              3-7
-------
combustible gases.  Process upsets and operating problems can
occur at any pulp mill, and fans have been reported to be the
spark source for explosions in transport systems where design
flaws, inadequate maintenance, or improper operation allowed
explosive gases to enter a fan that was designed for handling
gases below their lower explosion limit (LEL).10
     Explosion proof motors can be used; however, based on the
concentrations of organics in the vent gases, the vent streams
from points examined in this document would be below the LEL.
In some cases, such as with low-volume, high-concentration
(LVHC) streams (e.g., weak liquor storage tank vent stream),
the gas concentration may exceed 25 percent of the LEL, the
typical safety guideline level.11  The explosive potential
of the vent streams varies greatly depending on the
concentration of turpentine.  Flame arrestors have been
incorporated into the duct design as a safety precaution.
     Steam ejectors are preferred as prime movers in transport
systems handling high-concentration NCG's.  Steam ejectors
eliminate the source of sparks from the system and provide
dilution of NCG's with steam, which lowers the LEL.  However,
steam ejectors require a significant amount of steam, which is
subsequently vented to the control device.  Because of the
potential impact of this steam on the control device, such as
reduced heat content and increased volume of vent streams,
steam ejectors are not normally used on high-volume, low-
concentration (HVLC) vent streams.12
     Vent gas may be conditioned to alter the moisture content
or the temperature of the stream before it is vented to the
control device.  This may be accomplished using condensers,
knockout drums, or entrainment separators in the gas transport
system.
     Preheating of vent gases is only performed when the
stream is controlled with a combustion device.  Vent streams
may be preheated if their volumetric flow rates are large
enough to affect combustion in the control device.  Preheating
                              3-8
-------
is generally only practiced on HVLC streams or streams with
little or no turpentine, where the risk of explosion is
sufficiently low.13  Preheating would therefore be more
applicable for streams such as knotter and washer vent streams
in hardwood pulping processes and softwood pulping processes,
where the turpentine concentration is sufficiently below the
LEL.  For this analysis, no preheating was assumed.
     When ducting vent streams that contain potentially
explosive compound concentrations, safety devices must be
incorporated into the gas transport system.  Flame arresters
and rupture discs are components typically found in transport
systems.  Flame arresters prevent the propagation of fires
through the duct system.  Rupture discs are used to prevent
damage to the gas transport system by rapidly venting gases
during explosions.  Monitoring equipment may also be used to
provide real-time observations of vent stream parameters such
as temperature and volume percent of combustible compounds
(percent LEL).
3.2.2  Applicable Vent Control Devices
     3.2.2.1  Combustion Control Devices.  Combustio_n control
devices destroy the chemical structure of the organic compound
by oxidation at elevated temperatures.  These devices operate
on the principle that any VOC heated to a high enough
temperature in the presence of sufficient oxygen will oxidize
to carbon dioxide and water.14  Combustion devices have been
documented to control organic compounds by at least 98 percent
under a wide range of vent stream and VOC characteristics.15
     Two strategies are used in controlling vent gases with
combustion devices.  First,  the vent gas stream may be used as
auxiliary fuel if the stream has a high enough heat content
(approximately 100 Btu/scf or greater).16'17  Secondly,
the vent gas stream may be used as combustion air if the
stream has sufficient oxygen content (approximately
20 percent).
     Because the basic operating principle of the various
combustion control devices is similar, the factors that affect
                              3-9
-------
their destruction efficiency are also.similar.  The
destruction efficiency of-these devices is a function of the
temperature of the combustion chamber (or zone),  the residence
time of the pollutant in the combustion chamber,  and the
mixing in the combustion chamber of the pollutant, oxygen, and
the hot gases generated by combustion.14  Typical residence
times for incinerators achieving at least 98 percent
destruction efficiencies range from 0.25 to 1.5 seconds.18
The temperature of the combustion chamber depends on the
amount and heat content of the fuel burned, the percent excess
air, the moisture content of the stream, and the amount of •
oxygen.
     Applicable combustion devices discussed in this section
include lime kilns, power boilers, recovery furnaces, thermal
incinerators, and flares.  Properly operated, each of these
combustion devices can achieve destruction efficiencies of
98 percent or greater.
     The lime kiln, power boiler, and recovery furnace are
integral to mill processes.  However, vent streams may be
routed to these devices without interfering with the normal
operation of the process.  Mill combustion devices such as
lime kilns and power boilers are occasionally shut down
because of process upsets or maintenance.  During this time,
these devices will not be available to control vent gases.
However, interruptions in combustion device service jnay also
correspond with suspension of the processes that generate the
emissions.  For example, a mill may halt pulping processes
(e.g., digestion) shortly after its recovery furnace goes down
because of limited liquor reserve.  Available data show an
average unscheduled downtime between 1 and 5 percent for pulp
mill combustion devices.19  For costing purposes, these
devices were assumed to operate 350 days per year.
     3.2.2.1.1  Lime kiln.  The lime kiln is an essential
element of the causticizing cycle, and is used to calcine lime
mud (calcium carbonate) to produce calcium oxide.  The high
temperatures encountered in the lime kiln  (950 to 1,250°C)
                              3-10
-------
make it very efficient in destroying VOC, with control
efficiencies reported to be greater than 98 percent.
     The lime kiln has been demonstrated in the pulp industry
as a control device for LVHC emission points such as digester
relief gases, digester blow gases, turpentine recovery system
NCG's, and evaporator vent gases.  These LVHC vent gas streams
are generally used as supplementary fuel because these streams
have been demonstrated to contain sufficient heat content.
However, these vent streams may exceed the LEL if high levels
of turpentine are present.  Preheating of the vent gases is
generally not practiced because of the risk of explosions from
the turpentine in the vent stream.13  The volumetric flow rate
generated by typical pulp washers is usually too large to vent
to the lime kiln.  Therefore, the lime kiln may be less
applicable for controlling HVLG vent streams.
     The cross-media impacts resulting from venting HAP
emission points to the lime kiln are the generation of the
HAP-laden liquid stream from any gas conditioning equipment
used (i.e., entrainment separator, condenser, or knock-out
drum) and a potential increase in sulfur oxides emissions from
the kiln exhaust due to the TRS compounds in the pulping vent
streams.  The condensate streams may be recycled back to mill
processes (e.g., pulp washers)  or sent to wastewater treatment
depending on the volumes and characteristics of the wastewater
generated.
     3.2.2.1.2  Power boiler.  Power boilers, which include
coal, natural gas, oil,  wood waste,  or combination fuel-fired
boilers, are designed to produce heat, steam, and electricity
for mill operations.   Power boilers with capacities greater
than or equal to 150 million Btu/hr operate at high -
temperatures (generally greater than 1,000°C) and can serve as
excellent control devices, providing at least 98 percent
destruction of VOC.20
     Power boilers have been demonstrated in the pulp industry
as a control device for pulping vent emission points,  and may
be preferred over the lime kiln for burning vent gases because
                             3-11
-------
they have less downtime and can handle larger vent gas volumes
than the lime kiln.21
     The vent gas stream is generally used as part or all of
the combustion air needed by the boiler,  although the stream
may also serve as auxiliary fuel.22  The emission points
vented to the power boiler are both LVHC and HVLC streams such
as digester relief and blow gases, turpentine recovery system,
evaporator, and pulp washer hood vent gases.  However, streams
that contain high levels of turpentine, such as digester
relief and blow gases from softwood pulping, may approach the
LEL, and are more often vented to the lime kiln instead of to
the power boiler.  Other streams contain methanol and TRS,
which at the reported concentrations in the HVLC streams,
would be below the LEL yet still have some fuel value.  The
fuel credit from the heat of combustion of the organics in the
stream, as well as the fuel penalty of heating the stream's
moisture and air to combustion temperatures, were considered
when venting these streams to existing combustion devices.23
     Power boilers are not currently applied to control the
unscrubbed halogenated vent gases associated with the
bleaching process.  However, a halogenated stream may first be
scrubbed to remove the majority of the halogens prior to
combustion.  The impacts of venting chlorinated streams to the
power boiler have not been fully evaluated.  However, the
introduction of bleach plant vent streams would likely result
in an accelerated corrosion rate of the boiler.
     Information detailing the use of gas conditioning
techniques for vents ducted to power boilers is not available.
The assumptions and basis for venting gas streams to an
existing combustion device are discussed in Chapter 5.0.  The
cross-media impacts resulting from venting HAP emission points
to the power boiler are identical to those discussed for lime
kilns in Section 3.2.2.1.1.
     3.2.2.1.3  Recovery furnace.  The recovery furnace is the
heart of the kraft liguor recovery process, and is used to
recover the chemicals used in cooking liquor.  Furnaces
                              3-12
-------
generally serve as excellent control devices, providing at
least a 98 percent destruction of VOC because of their high
operating temperatures  (generally exceeding 1,000°C).15
     The recovery furnace has been demonstrated in the pulp
industry as a control device for HVLC emission points.
However, this combustion device is generally not preferred for
controlling vent gases with high levels of turpentine because
of the risk of explosions.  The vent gases controlled by the
recovery furnace should be conditioned to remove moisture
because water may react violently with the smelt bed" in the
furnace.15  The vent streams controlled in the recovery
furnace would have similar characteristics and LEL to those
controlled in the power boiler.
     Recovery furnaces do not currently receive the unscrubbed
halogenated vent gases associated with the bleaching process.
However, a halogenated stream may first be scrubbed to remove
the majority of the halogens prior to combustion.  The impacts
of venting chlorinated streams to the recovery furnace have
not been fully evaluated.
     The cross-media impacts resulting from venting HAP
emission points to the recovery furnace are similar to those
of lime kilns, as discussed in Section 3.2.2.1.1.
     3.2.2.1.4  Thermal incinerator.  Thermal incinerators
operate on the principle that any VOC will oxidize to carbon
dioxide and water if heated to a high enough temperature in
the presence of a sufficient amount of oxygen.24  A thermal
incinerator is a refractory-lined chamber containing a burner
or burners used to oxidize VOC-containing vent streams.
Although there are many different incinerator designs, an
example incinerator is shown in Figure 3-1.  A discrete
dual-fuel burner,  an inlet for the vent stream, and a
combustion air inlet are arranged in a premixing chamber to
ensure thorough mixing.  The mixture of hot combusting gases
then passes into the main combustion chamber.  This chamber is
sized to allow the mixture enough time at the elevated
temperature for oxidation to reach completion (residence times
                             3-13
-------
                                                                                       Stack
    Vent Stream
       Inlet
        (2)
Auxilllary
 Burner
(Discrete)
  (1)
                                                                           Optional Hot
                                                                            Recovery
                                                                               (6)
                  Figure 3-1.  Discrete Burner, Thermal Incinerator
                                           3-14
-------
of 0.3 to 1.0 seconds are common).  Performance tests have
demonstrated that properly operated thermal incinerators can
achieve 98 percent or greater destruction efficiency for most
VOC.15
     Incinerators have been demonstrated in the pulp industry
as an applicable control device for reducing gaseous
emissions, and can be designed to control both LVHC and HVLC
vent streams.  Package single-unit thermal incinerators exist
that can control streams with flow rates in the range of 14 to
1,400 standard cubic meters per minute (500 to 50,000 standard
cubic feet per minute). However, combustion of a vent stream
with a heat content less than approximately 100 Btu/scf, such
as vent streams from the pulp washers, usually requires
burning supplemental fuel to maintain the desired combustion
temperature.4 / ! 5
     Incinerators can be used in conjunction with gas
absorbers to reduce HAP emissions from bleach plant vents.
However, thermal oxidation of halogenated VOC requires higher
temperatures to oxidize the halogenated organic compounds.
The halogenated exhaust streams from the incinerator are
quenched in order to lower their temperature and then routed
through absorption equipment, such as a packed tower
scrubber.25  Section 3.2.3.2.3 discusses the operation and
application of absorption equipment.
     It has been reported in a literature survey that some
mills (approximately 33 percent of the mills that responded to
the survey)  use entrainment separators to remove .moisture from
the vent gas prior to venting to an incinerator.26  Loss of
flame due to excessive moisture was also reported in the
survey.27  It is not known whether preheating of the vent
gas is practiced with the use of an incinerator.  Although
incinerators can be designed with heat recovery to reduce
auxiliary fuel costs, none of the facilities that responded to
the survey use heat recovery because of the risk of -
explosions.2^
                             3-15
-------
     Cross-media impacts resulting, from venting emission
points to an incinerator involve the liquid stream generated
from the gas-conditioning equipment used to remove moisture
from the vent stream, and potentially unburned hydrocarbons,
nitrogen oxide, carbon monoxide, and sulfur oxides emissions
associated with the incinerator exhaust.  The impact of
condensate streams has not been fully evaluated.  These
streams may be recycled back to mill processes  (e.g., pulp
washers) or sent to wastewater treatment, depending .on the
volumes generated.  If a gas scrubber is used to remove acid
gases from incinerator exhaust, brine solution, formed when
neutralizing acid gases with caustic solution, must be
disposed of, and is typically sent to the wastewater treatment
system.
     3.2.2.1.5  Flare.  Flares are open combustion devices in
which the oxygen necessary for combustion is provided by the
ambient air in the proximity of the flame.  Properly operated,
flares have been shown to have VOC/HAP destruction
efficiencies of 98 percent or greater.28  Flares are capable
of accepting fluctuations in VOC concentration and flow rate
and are applicable for continuous, batch, and variable flow
rate vent stream applications.  However, sufficient heat
content is necessary in the vent stream for proper operation.
For this reason, flares are only used as backup systems at a
few facilities in the pulp industry to primary combustion
devices such as lime kilns.
     3.2.2.2  Gas absorbers.  Gas absorbers are used to
recover sulfur dioxide from sulfite mill pulping vents and to
control chorine, hydrochloric acid, and chlorine dioxide in
bleach plant vent streams.  Polar organic compounds such as
methanol are also removed.  This section only discusses bleach
plant scrubbers because sulfite pulping vent scrubbers are an
integral part of the chemical recovery process.
     In the absorption process, soluble components of a waste
gas mixture are dissolved in the scrubbing medium.  The
pollutant diffuses from the gas into the caustic solution when
                              3-16
-------
the liquid contains less than the equilibrium concentration of
the gaseous component.  The difference between the actual
concentration and the equilibrium concentration provides the
driving force for absorption.29
     Figure 3-2 presents a schematic of a packed absorption
tower using countercurrent flow.  The vent stream containing
compounds to be absorbed is introduced near the bottom of the
tower, passes through the packing material, and exits the
tower near the top.  The packing in the absorber tower helps
to increase contact between the soluble compounds and the
absorbing solution.  The absorbing solution flows from the top
of the column, countercurrent to the vapors, absorbing the
solute from the gas phase.29  The absorbing solution used in
pulp mill bleach plant scrubbers is typically caustic and
originates from bleach plant extraction stage filtrates
(i.e., the caustic sewer), weak wash from the chemical
recovery process, white liquor, sodium bisulfite (a byproduct
from some chemical manufacturing operations), or from fresh
caustic solution.  Other media used include sulfur dioxide and
chilled water.30
     Removal efficiencies for gas absorbers vary based on
column design, the type of absorbing solution, and the
solubility of the compound being absorbed.  Chlorine removal
efficiencies as high as 99 percent have been documented with a
caustic solution.30  The chlorine reacts to form sodium
chloride and sodium hypochloride.
     Removal efficiencies for other compounds range from 0 to
99 percent.  For example, polar compounds such as methanol
approach 99 percent removal,  and compounds such as chloroform
have insignificant (approximately 0 percent) removal.31
However, absorbed compounds such as methanol may volatilize
back into the atmosphere from the waste treatment process,
thus lowering the overall efficiencies of the scrubber as an
air control device.
     Using an Advanced System for Process Engineering (ASPEN)
modeling approach, the scrubber removal efficiencies for
                             3-17
-------
                                                               (5) Cleaned G*» Out
                                                               to Final Control Device
                                                                 or to Atmosphere
Absorbing
 Liquid In
(3)
                                                                      T\   (1) VOC-Uden
                                                                      \-	  Gaeln
                                        Absorbing Uquid
                                     with VOC out to Disposal
                                     or VOC/Solvent Racovary
              Figure 3-2.  Packed Tower Absorption Process
                                        3-18
-------
specific compounds were estimated.31  Tne emissions from the
scrubber effluent  (due to volatilization) were then estimated
to approximate a net emission reduction.31  Table 3-4 presents
the'modeled scrubber removal efficiencies and net emission
reductions.
     The cross-media impact associated with using gas
absorbers with a caustic solution is the production of a brine
solution.  This solution is typically sewered with the bleach
plant effluent into the wastewater treatment operations.  This
impact is discussed in Chapter 4.0.  Some facilities use fresh
caustic as the scrubbing medium and use the scrubber effluent
in the extraction stage of the bleaching process.
     3.2.2.3  Condensers.  Moisture, VOC, and volatile HAP's
can be removed from vent streams using condensation.  In this
technique, VOC, HAP and moisture are separated from vent
streams by lowering the gas temperature enough to create a
change from gas to liquid phase.  In a two-component system
where one of the components is non-condensible (e.g., air),
condensation occurs at dew point (saturation) when the partial
pressure of the volatile compound is equal to its vapor
pressure.  Condenser flow capacities are typically limited to
approximately 57 scmm (2,000 scfm) for a single unit-.32
     Condensers are currently used in the pulp industry
primarily to condition vent gases by removing moisture.
Organics, such as turpentine, can also be recovered from
digester blow gases using condensers.  The removal efficiency
of condensers varies, but can achieve as high as 90 percent in
some cases.33  Condensers may also be used as supplemental
control techniques to lower moisture content and remove
potentially explosive organic compounds from LVHC and HVLC
streams before they are sent to the primary control device.
The resulting condensate streams may be recycled back to mill
processes (e.g.,  pulp washers), steam stripped, or sent to
wastewater treatment, depending on the volumes generated.
                              3-19
-------
           TABLE 3-4.  SCRUBBER REDUCTION ESTIMATES
                                  Estimated
                                   Scrubber         Estimated
   Compound Classification3      Removal  (%)b     Reduction (%)c


 Chlorine                              99            -   99

 High  Solubility                       99                75
  Methanol
  Acetone
  Formaldehyde
  2,4,5-Trichlorophenol
  Pentachlorophenol
  Chlorophenolics
  Hydrochloric  Acid
  Chlorine  Dioxide

 Medium Solubility                     60                35
  Methyl Ethyl  Ketone
  Acrolein
  Acetaldehyde
  Propionaldehyde
  Dichloroacetaldehyde

 Low Solubility                       0                0
  Chloroform
  Carbon Tetrachloride
  Methylene Chloride
  Toluene
  1,1,1-Trichloroethane
  Alpha-Pinene
  Beta-Pinene
  Chloromethane
  p-Cymene

 Average			70	

a  Compounds  are  classified by solubility.   High-solubility
   compounds  have solubilities greater than  or equal  to
   methanol;  low-solubility compounds have solubilities less
   than or  equal  to  chloroform; medium-solubility compounds
   were between methanol and chloroform.

b  Based on a model  scrubber designed to  remove 99 percent of
   the chlorine,  99  percent of the methanol  was removed and
   less than  1  percent  of the chloroform  was removed.
   (Reference 30)

c  The volatility of the speciated compounds was evaluated and
   a  fraction emitted was estimated based on the mass removed -
   in the scrubber effluent.
                             3-20
-------
     3.2.2.4  Adsorbers.  Carbon adsorbers are not currently
used in the pulp industry, although regenerative carbon
adsorbers, in conjunction with incineration, can be used to
control HVLC vent streams.
3.3  APPLICABLE CONTROL TECHNIQUES FOR WASTEWATER EMISSION
POINTS
     In wood pulping, bleaching, and chemical recovery
processes, wastewater streams containing HAP compounds are
generated." Generally, wastewater passes through a series of
collection units before being sent to treatment units.  Many
of the collection system units are open to the atmosphere and
allow some of the HAP's to be emitted to the ambient air.34
This section discusses control devices used to reduce HAP
emissions from wastewater points. Section 3.3.1 briefly
describes the techniques used to reduce HAP emissions from the
wastewater collection system.  Sections 3.3.2 and 3.3.3
discuss steam and air strippers with vent control,
respectively.
3.3.1 , Wastewater Collection System
     To reduce HAP emissions from the pulping and bleaching
wastewater points described in Chapter 2.0, the collection
system that conveys the wastewaters to treatment operations
(including strippers) should be designed in such a way as to
reduce the amount of contact between the HAP-containing
wastewater and the ambient air.  This can be accomplished by
using covers and water seals on collection system
components.35  Hard-piping the wastewater point to the
treatment system or control device provides the best control
of HAP emissions from wastewater.36
3.3.2  Steam Stripper with Vent Control
     Steam strippers are currently used to reduce organic and
sulfur compound loading in condensate streams generated by the
pulping processes.   Steam stripping involves the fractional
distillation of wastewater to remove organic compounds.  The
basic operating principle of steam stripping is the direct
contact of steam with wastewater.  This contact provides heat
for vaporization of the more volatile organic compounds.37
                             3-21
-------
At a pulp mill, the steam stripper can be a stand-alone system
or it can be integrated into the evaporator effects.
     In the stand-alone steam stripping process, wastewater
containing organic compounds is pumped to the stripping
column.  Heat is provided to the stripping column by direct
injection of steam into the bottom of the column.38
Generally, steam stripping columns are equipped with trays or
packing to provide contact between the vapor and liquid
phases.  In the pulp industry, the overhead vapor stream
containing organics and water is typically partially
condensed, with the condensate routed back to the stripper
column as reflux.  The vapor stream is then incinerated in an
on-site combustion device, as described in Section 3.2.2.39
The treated wastewater stream is passed through a heat
exchanger that cools the treated wastewater and preheats the
stripper feed stream.  The stripped wastewater is either
reused in the process (i.e., as wash water) or discharged to
wastewater treatment operations.
     Alternatively, a steam stripper can be integrated with
the evaporator set, as shown in Figure 3-3.  In this case, the
overhead vapor stream, which is predominantly steam, is routed
to the next effects.  A reflux tank is also incorporated to
direct the bottoms from the upstream effect into the- steam
stripper.  The vent gases from the reflux tank are typically
sent to a combustion device.
     Achievable VOC and HAP emission reductions are highly
dependent on wastewater characteristics, such as,organic
concentration and composition, and the design and operation of
the stripper as well as the collection and treatment systems.
Steam stripper removal efficiencies ranging from 75 to
99 percent have been reported in the literature.40
     The steam stripper design and operating parameters that
have the greatest effect on the removal performance of organic
compounds are the number of trays (or height of packing) and
the steam-to-feed ratio (SFR).  In general, the removal
efficiency increases as the number of trays (height of
packing) increases.   (For a given stripper system, there will
                              3-22
-------
                                               8438418RTP
                     H
                                      ill"
- o +
2«Z
|is
                                      LU
                                         \
                                              "S
                       Q.W

                       +^
                       (A
                                   II
                                   o i
                                   i-g
                                   CO X
                                   5"1
                                   *I
                                eg
.1
11
                                        s
                               -ii ^
                               M  UJ
                                              AS  Q*

                                              ^  W

                                              S  o
                                                           w
                                                           w.
                                                           o
                                                           a
                                                           Q.
                                                           'l_
                                                           •M
                                                           C/D
                                                         03
                                                         0)
                                                         •«-«
                                                         C/)

                                                         T3
                                                         (U
                                                         +-<
                                                         (U
                                                         k_
                                                         O)
                                                         0)
                                                         V)
                                                         3
                                                         O
                                                         3
                                                         _C
                                                         '•P
                                                         C
                                                         O
                                                         O
                                                           CO

                                                           CO

                                                           
-------
be a maximum number of trays (packing height)  beyond which no
additional removal will be achieved.)
     An increase in the SFR ratio will increase the ratio of
the vapor-to-liquid flow through the column.  This increases
the stripping of organics into the vapor phase.  Because
additional heat is provided when the steam rate is increased,
additional water is also volatilized.  Therefore, an increase
in the SFR ratio is also normally accompanied by an increase
in the steam rate flowing out of the column in the overhead
stream.41
     Based on responses to an industry survey, the average SFR
used for controlling pulping wastewater streams is
1.5 Ib. stream/gal, wastewater.42  The Kremser equation was
then used to generate a relationship between the fraction of
compound removed (Fr) and compound Henry's Law constant at an
SFR of 1.5 lb/gal.42  These Fr's are summarized in Table 3-5.
Predicted HAP removals at an SFR of 1.5 lb/gal range from 90
to 99 percent.42
     Steam strippers are currently used in the pulp industry
to reduce TRS and organic compound loading in pulping process
and chemical recovery evaporator wastewater or condensates.
Typically, steam stripping is applied to condensate streams
from'the blow tank, turpentine recovery system, and the
eyaporators.  Liquid streams from any gas-conditioning
equipment used to remove moisture from vent gases may also be
stripped to remove organics before being sewered.
     The cross-media impacts associated with the use of steam
strippers involve the organic-laden vent stream and stripped
wastewater stream.  Criteria pollutants (i.e., sulfur dioxide,
oxides of nitrogen, carbon monoxide and particulates) will
also be emitted from the fossil fuel burning required to
generate the steam tot operate the stripper.  Sludges may be
generated from the feed tanks and must be disposed.  For this
analysis, no auxiliary fuel is necessary for burning the steam
stripper overheads vent stream because the heat content of
this stream offsets the fuel required to bring to combustion
temperature.23
                             3-24
-------
        TABLE  3-5.   STEAM STRIPPER  REMOVAL EFFICIENCIES

	HAP  Compound	Removal Efficiency5	
 Acetaldehyde                                  99
 Acrolein                                      99
 2-Butanone  (MEK)                              99
 Formaldehyde                                  99
 Methanol                                      90
 Propionaldehyde                               99
 Total  Reduced Sulfur  (TRS)	9j4b	
a  Removal  efficiency  is based on a steam-to-feed ratio of
   1.5  pounds  of  steam per gallon of wastewater.
   (Reference  42)
0  Removal  efficiency  for TRS is based on the. average removal
   efficiencies for hydrogen sulfide,  dimethyl disulfide,
   dimethyl  sulfide, and methyl mercaptan.
                             3-25
-------
3.3.3  Air Stripper with Vent Control
     Another control technique for reducing HAP emissions from
wastewater is air stripping.  The underlying principle for air
stripping is vapor-liquid equilibrium.  By forcing large
volumes of air through the contaminated water, the air-water
interface is increased, resulting in an increase in the
transfer rate of the organic compounds into the vapor
phase.43  The overhead vent stream is then sent to a
combustion device.
     Although air strippers have been employed in the pulp
industry to reduce TRS emissions, the organic concentrations
in the condensate streams from the blow tank, turpentine
recovery operations, and evaporators are generally too high to
be effectively controlled by an air stripper.
                              3-26
-------
3.4  REFERENCES

1.    Summary of Technologies for the Control and Reduction of
     Chlorinated Organics from the Bleach Chemical Pulping
     Subcategories of the Pulp and Paper Industry.
     U. S. Environmental Protection Agency, Office of Water
     Regulations and Standards.  Washington, D.C.  April 27,
     1990.  pp. 20, 22, 25 through 27, 43, 54, and 63.

2.    Responses to Industry Survey discussed in the following
     letter:  J.E. Pinkerton, National Council of the Paper
     Industry for Air and Stream Improvement, Incorporated
     (NCASI), to J. Telander, EPA: 15B, and P. Lassiter, EPA:
     CPB.  February 11, 1992.  (Responses were claimed
     confidential business information).

3.    Environmental Pollution Control, Pulp and Paper Industry,
     Part lr Air.  U.S. Environmental Protection Agency.
     Technology Transfer.  Publication No. EPA/625/7-76-001.
     October 1976. p. 1-4.

4.    Memorandum from Greene, D.B., Radian Corporation, to
     Shedd, S.A., EPA/CPB.  Heat Release Factors.
     September 30, 1993.

5.    Committee on Industrial Ventilation.  Industrial
     Ventilation. 19th Edition.  Ann Arbor, Michigan, Edwards
     Brothers Incorporated.  1986.  p. 4-1.

6.    Cooper, C.D. and F.C. Alley.  Air Pollution Control:  A
     Design Approach.  Boston, PWS Engineering.  1986.
     pp. 219-220.

7.    Memorandum from Greene, D.G., Radian Corporation, to Pulp
     and Paper NESHAP File.  Brownstock Washer Enclosure
     Costs.  July 21, 1993.

8.    Collection and Burning of Kraft Non-Condensible Gases -
     Current Practices, Operating Experience, and Important
     Aspects of Design and Operation.  Technical Bulletin
     No. 469.  New York, National Council of the Paper
     Industry for Air and Stream Improvement, Inc.  August 29,
     1985.  p. 40.

9.    An Investigation of Corrosion in Particulate Control
     Equipment.  U. S. Environmental Protection Agency, Office
     of General Enforcement.  Washington, DC.  Publication
     No. EPA-340/1-81-002.  February 1981.  p. 38.

10.  Ref. 8, p. 41.
                             3-27
-------
11.  OAQPS Control Cost Manual.  Fourth Edition.
     U. S. Environmental Protection Agency, Office of Air
     Quality Planning and Standards.  Research Triangle Park,
     NC.  Publication No. EPA 450/3-90-006.  January 1990.
     p. 3-26.

12.  Ref. 8, p. 42.

13.  Ref. 8, p. 51.

14.  Hazardous Air Pollutant Emissions from Process Units in
     the Synthetic Organic Chemical Manufacturing Industry—
     Background Information for Proposed Standard.  Volume IB,
     Control Technologies.  U. S. Environmental Protection
     Agency, Office of Air Quality Planning and Standards.
     Research Triangle Park, NC.  EPA-453/D-92-0166.
     November 1992.  pp. 2-8 and 2-9.

15.  Memorandum from Farmer, Jack R., EPA/CPB to Ajax, B., et
     al., EPA/CPB.  Thermal Incinerators and Flares.
     August 22, 1980.

16.  Ref. 8, p. 50

17.  Memorandum from Pandullo, R.F., Radian Corporation, to
     Barbour, W.,  Radian Corporation, Evans, L., U.S. EPA, et
     al.  Summary of April 11 Meeting to Discuss Thermal
     Incinerator Cost Issues.  April 27, 1990.

18.  Ref. 14, pp.  2-12 and 2-18.

19.  Telecon.  Bagley, C.J., Radian Corporation, with Holt,
     J., Hartford Steam Boiler, July 19, 1993.  Discussion of
     Percent Downtime.

20.  Ref. 14, p. 2-18.

21.  Ref. 8, p. 56.

22.  Memorandum from Seaman, J.C., Radian Corporation, to
     Project File.  Control of Pulping Vent Streams in an
     Existing Combustion Device.  September 29, 1993.

23.  Memorandum from Greene, D.B., Radian Corporation, to
     Project File.  Fuel Penalty.  October 8, 1993.

24.  Ref. 14, p. 2-7.

25.  Ref. 14, p. 2-10.

26.  Ref. 8, p. 59.

27.  Ref. 8, p. 60.

28.  Ref. 14, p. 2-6.

                              3-28
-------
29.  Ref. 14, pp. 2-48 and 2-49.

30.  Bleach Plant Chlorine and Chlorine Dioxide Emissions and
     Their Control.  Technical Bulletin No. 616.  New York,
     National Council of the Paper Industry for Air and Stream
     Improvement, Inc., September 1991.  pp 2 to 10.

31.  Memorandum from Olsen, T.R., Radian Corporation, to
     Shedd, S.A., EPA/CPB.  Model Scrubber Removal
     Efficiencies.  September 17, 1993.

32.  Ref. 14, p. 2-33.

33.  Control Technologies for Hazardous Air Pollutants
     Handbook.  Air and Energy Engineering Research Laboratory
     Office of Research and Development.  U. S. Environmental
     Protection Agency, Research Triangle Park, NC.
     EPA/625/6-86/014.  September 1986.  p. 27.

34.  Industrial Wastewater Volatile Organic Compound
     Emissions — Background Information for BACT/LAER
     Determinations.  U. S. Environmental Protection Agency,
     Control Technology Center.  Research Triangle Park, NC.
     Publication No. EPA-450/3-90-004 .   January 1990.  p. 3-2
     and 3-3.
35.
36.
37.
38.
39.
40.
41.
42.
Ref.
Ref.
Ref.
Ref.
Ref.
Ref.
Ref.
34
34
34
34
8,
34
34
/ P-
/ P-
/ P-
/ P-
P-
/ P-
, P-
Memorandum
4-20.
4-22.
4-3.
4-4.
30.
4-14.
4-13.
from F
     Pulp and Paper NESHAP Project File.  Design Steam-to-Feed
     Ration of a Steam Stripper in Pulp Mills and Development
     of Fraction Removed Values.  September 3, 1993.

43.  Ref. 34, p. 4-18.
                             3-29
-------
         4.0  MODEL  PROCESS UNITS, CONTROL OPTIONS, AND
                      ENVIRONMENTAL IMPACTS
     This chapter defines the model process units that were
developed to analyze environmental and cost impacts on the
pulp industry, the emission control options that were
selected, and the environmental impacts of applying these
controls to an example facility.  Model process units are
parametric descriptions of the types of processes that exist
and that are likely to be constructed in the future.  Control
options are the set of demonstrated emission control
techniques currently being evaluated in analyzing the MACT.
The environmental impacts for these options include air,
water, energy, and other impacts.
     Section 4.1 describes the model process units developed
for pulping and bleaching operations and how the units were
used to estimate national emissions.  The emission control
options and environmental impacts for an example mill are
presented in Section 4.2 and Section 4.3, respectively.
4.1  MODEL PROCESS UNITS
     This section presents a discussion of the development of
model process units and a brief description of how these
models were used in estimating national emissions and impacts
of control options.  For the purpose of the analysis, the
emission points within the scope of this document were divided
into pulping and bleaching areas (as discussed in
Chapter 2.0).  The pulping area represents the pulping and
washing processes, as well as chemical recovery through
evaporation and oxygen delignification processes (where
applicable).   The bleaching area represents the chemical
bleaching process.  Industry has commented that the pulping
and bleaching models used to analyze the environmental and

                              4-1
-------
cost impacts do not represent the variability of emissions
within the pulp industry.  Industry is currently conducting a
test program and all data provided to the EPA in a timely
manner will be considered for review and incorporation into
the final regulatory alternatives.  Development of the pulping
model process units is discussed in Section 4.1.1, and
development of the bleaching model process units is discussed
in Section 4.1.2.  Section 4.1.3 briefly discusses the
assignment of pulping and bleaching model process units to
pulp mills within the industry for estimating national
emissions and control impacts.
4.1.1  Pulping Model Process Units
     Existing literature and source test data were used to
develop air emission factors, as presented in Appendices B and
C and Chapter 2.0.  These data were evaluated to determine
which parameters of the pulping process affect HAP emissions.
Table 4-1 identifies seven parameters that have an effect on
HAP emissions.  Some of these parameters (e.g., pulping
process, wood type, and pulp production capacity) affect the
nature and quantity of the HAP formed and, therefore,
potentially emitted.  Other parameters (e.g., washer type, and
digestion process) affect the concentration and flow rate of
the emission point- vent streams and, therefore, affect the
control of these streams.
     Eighteen model units were developed to characterize the
pulping process area.I/2  Table 4-2 describes each model unit
and presents total uncontrolled HAP emission factors.  The
uncontrolled HAP emission factors were developed from the sum
of individual HAP compound emission factors for both process
vent and wastewater emission points.  Speciated HAP, total
volatile organic compounds (VOC), and total reduced sulfur
(TRS) emission factors are presented in Appendix C for each
emission point for these 18 model process units.  In addition,
other vent stream and wastewater stream characteristics
(e.g., flow rate and concentration) are presented in
Appendix C.  As shown in Table 4-2, the total uncontrolled HAP
                              4-2
-------
          TABLE 4-1.
PULPING PROCESS CHARACTERISTICS
     AFFECTING EMISSIONS
    Process characteristics
                Process parameters
 Chemical pulping process

 Wood type

 Digestion process

 Washer type

 Additional delignification
 Coproduct recovery

 Capacity
          Kraft/soda
          Sulfite
          Semichemical
          Softwood
          Hardwood
          Batch
          Continuous
          Vacuum drum
          Improved washing3
          Oxygen delignification
          Turpentine
          Tall oil
          Pulp production capacity
a  Horizontal belt, diffusion, and baffle washer systems
   affected emissions in a similar manner (i.e., enclosed
   versus open or hooded).
                              4-3
-------














CQ
H
§
[i PROCESS
H
Q
0


O

H
04
J
D
Pi


N
1
*
H
i











73 C •—
(u o a
i«{ ,f~\ i
o w £ a
SH "H I,
•P g "B &
C 0) $ 5^

O ft ^ CT>
£3 ^
hJ W ^^
C
O
V> "cT
j- id 2
l£°
0 G M
u CP 0)
rH >-^
CU
•c
Washer
type

rH >i
jW 1,
ID M
_j 2?
"3 o
n\ M
r* fl!
fi i
U H

•O Q)
o a
O >i




* i Q)
to §;
cu £
_i
•H
Q
en
C f\\
•H o
£*
3 "*"*
ft

CO
rH 10 ^j
TJ O'c
o o 5
gt 1 #^
W
•

CN o> o
O CT> C\
• • •
in H •<*







000
222



"3 m
cre E7e §i|
m 3 nj 3 o?
4J ^ JJ ^ fc -^
0 T3 O 73 a £
a « e 2
H •*


4J -P -P
(4^ <^| (4^
(0 nj (0
t 1 ^ [ t 1
1*1 M yj



T3 -P TS
^ *W >H
IT] O (0
X CO X

to
3
e ft 0
•g o g
-P -P .5
«j to n
03 m c
0
u

•P 4-* -P
Qi Qi li I
id id it]
M &6 X



rH fV] n
1 1 1
ft ft ft



in
o
•
in







O



id 3
o -o
PS


4J
(4-1
id
j_i
j<5



T3
^i
id
X

to
3
ntinuo
8

.p
id
US



•*
1
ft



•*
0^
•
H







O



Improved
washing


4J
-------
















««,
•O
9
•H
4J
a
o
o
CO
H
&

CO
CO
H
O
o
Pi
H
Q
i
o
2
H
Pi
D
Pi
•
CU
1
5f

H

"
















T3 C
CU O
H -H
r-l Ul
O Ul
-p'g
C CU
o
O 04
C* ^J
D EC


C
O
•H
C *
15
o E,
•H
rH
CU
•d
CU
r*
Ul
(0
S
rH
i
r4
CU
recox

CU
a

-P

o
Pj
^






.
*•»
ft
^
^*




%
§






n
H
in










to
CU


cu ?
° lc
W ff
pja
H •*
4J
«M
(0
r4
W

•d

(0
K
J3
O
4J
(0
CO





4J
^M
(0

}v]




n
H
1
04






VO
°l
l-l










Ul
CU


>c
^_J
o 2
r* m
g *>
H 3
4J
<(H
03
>H
«

4J

O
CO
£
O
-p
(0
0





-p

(0

W




H
1
04






CO
VO
•
^J<










Ul
CU


^^1
ti C
(0 3
-P >•

CU
-p
•H

VO
H










O
2


' ^C
>-H
Or
^ rn
ft (0
4J

•H
•P T3
C C
/t\ ^j
vl) *rt

rt
o
rH Ul
O
Ul -P
c o •
O (0 TJ
•H 
-------
emission factors vary from 1.05 to 5.16 kg HAP/Mg of pulp for
the model process units.   Other than pulping capacity,  the
factor that most affects  emissions is wood type,  with hardwood
emission factors (4.46 to 5.16 kg HAP/Mg)  being greater than
softwood emission factors (1.05 to 2.26 kg HAP/Mg).   Based on
available data, other parameters have little effect on total
pulping process emissions.
4.1.2  Bleaching Model Process Units
     Bleaching model process units were developed in a similar
manner as the pulping model process units described in the
previous section.  The bleaching process characteristics
determined to have the most effect on HAP emissions are wood
type, chemical use, and pulp bleaching capacity.   The use of
hypochlorite, chlorine, or chlorine dioxide was determined to
affect HAP emissions.
     From a review of available emissions data, twelve model
process units were developed to characterize the bleaching
area.1/2  Table 4-3 describes each of these model process
units and presents the total uncontrolled HAP emission factors
for each model.  The twelve models represent six bleaching
sequences for hardwood and six for softwood, with variations
in chemical use.
     The model emission factors presented in Table 4-3
represent the total uncontrolled bleach plant emissions from
both process vents and wastewater.  The process vents include
the tower vent, washer vent, and seal tank vent for each
bleaching stage.  The wastewater emission points include the
caustic sewer and acid sewer.  As shown in Table 4-3, the
bleach plant total HAP emission factors range from 0.56 to
2.11 kg HAP/Mg of pulp.  Similar to pulping, the hardwood
bleaching emission factors are generally higher than those for
softwood.  However, the greatest decrease in HAP emissions is
achieved through the elimination of all chlorine and
chlorinated compounds. Speciated HAP and total VOC emission
factors and other stream characteristics for each emission
                              4-6
-------
        TABLE 4-3.   BLEACHING MODEL PROCESS UNITS
Model
process
unit
B-l
B-2
B-3
B-4
B-5
B-6
B-7
B-8
B-9
B-10
B-ll
B-12
a Key:





Uncontrolled HAP
Bleaching sequence
(% C1O2 substitution)3
CEHD (0%)
CEHD (0%)
CEDED (0%)
CEDED (0%)
CdEDED (low)b
CdEDED (low)b
CdEDED (high)C
CdEDED (high)C
CdEDED (100%)
CdEDED (100%)
O-Ed
0-Ed
C = Chlorine
Cd = Chlorine dioxide
D = Chlorine dioxide
H = Hypochlorite
E = Extraction
0 = Oxygen/ozone
Wood
type
Hard
Soft
Hard
Soft
Hard
Soft
Hard
Soft
Hard
Soft
Hard
Soft

substituted




emission factor
(kg/Mg pulp)
1.98
1.30
1.75
1.06
2.11
1.04
1.67
1.45
1.66
1.45
0.56
0.59

for chlorine




A low substitution range is 10 to 50 percent substitution.
Less than 10 percent is considered to have the same
emissions as 0 percent substitution.
A high substitution range is 50 to 90 percent substitution.
Greater than 90 percent is considered to have the same
emissions as 100 percent substitution.
The totally chlorine free model bleaching sequence is used
in conjunction with oxygen delignification in the pulping
model process units.
                           4-7
-------
point for the twelve model process units are presented in
Appendix C.
4.1.3  Use of Model Process Units in Estimating National
Emissions
     To estimate emissions on a national level, model mills
were constructed using combinations of the 18 model pulping
and 12 model bleaching processes.  The composition and
distribution of these model mills were designed to approximate
the structure of the U.S. pulp industry.  A database
(discussed in Chapter 6.0) was assembled that contains
production information and the geographic location of each
wood pulp mill in the United States.  Production information
(including capacity, wood type, digestion type, washing type,
and bleach sequence) was used to assign appropriate model
pulping and bleaching units to individual mills.  Geographic
location was used to determine baseline control levels from
State regulations.  Section 4.1.3.1 discusses how the model
process units were assigned to pulping and bleaching lines at
individual mills and Section 4.1.3.2 summarizes how emissions
were estimated using these models.
     4.1.3.1  Model Assignment.  Pulping and bleaching model
process units were assigned to pulp mills within the industry
based on the criteria presented in Tables 4-2 and 4-3.
Because a mill could contain more than one pulping or
bleaching process, individual pulp and bleach lines were
evaluated for each facility.  A pulping line was defined as
the digesters associated with a specific washer.  In other
words, each line contained only one washer, but could contain
multiple digesters.  The pulping and bleaching model process
units were presented in Sections 4.1.1 and 4.1.2.  These
models were assigned on a pulp and bleach-line basis, and then
aggregated to represent the whole facility for each facility
in the industry data base.
                              4-8
-------
     4.1.3.2  Estimating Emissions.  Uncontrolled emissions
for model process unit emission points were calculated by
multiplying the assigned emission factors by the process unit
production capacity.  If the mill reported control of specific
points, or baseline controls were required by applicable State
or Federal regulations, baseline emissions were estimated by
adjusting the uncontrolled emissions with the documented
emission reduction efficiency of the assumed or documented
control device in place.  As discussed in Chapter 3.0, process
vents were assumed to use combustion technology or scrubbing
(sulfite mills); and a 98 percent organic HAP reduction
efficiency was applied.  Applicable wastewater points were
assumed to be controlled by a steam stripper achieving a 70 to
99 percent removal efficiency of individual HAP's, depending
on the pollutants present.  Applicable bleach plant points
were assumed to be controlled by a scrubber achieving 0 to
99 percent removal efficiency of individual HAP's, depending
on the pollutants present as discussed in Section 3.2.2.2 on
gas absorbers.  To obtain the total baseline emissions for a
process unit, emissions from individual streams were summed in
the same manner as for uncontrolled emissions.  Chapter 2.0
provides details on the basis for baseline controls in the
pulp and paper industry.
4.2  CONTROL OPTIONS
       Four control options are discussed in this document.
One option applies to all pulping vents, two options apply to
bleaching vents, and one option applies to pulping wastewater
streams.  Due to the high cost and low air emission
reductions, no control options are currently being evaluated
for bleaching wastewater streams.  Table 4-4 describes each
option, the control requirements, and specific emission points
to which the option applies.
     The control option for pulping vent emission points is
collection and conveyance to an existing combustion device
such as a power boiler or lime kiln (or scrubbing for sulfite
mills), assuming a 98-percent organic^reduction.  As discussed
                              4-9
-------




CO
4J
•rt
0
ft
C
O
01
01
u







C!
0 0)
•-4 O
01 Vl
01 3
"4 O
2 CQ
W




a
ca -
S?
8-
O<



^ C
^_
O ~j
0 C 4J
H Q) f»
.LJ "*^ 3
c . S *o
O Jj 0)
O Ll
H i M
0) „-
^




m
Costing basil





c
o
•*4
4J
o4








.* C C C
C 0 0 0 Vl
4J M-I 4J 4J 4J 4J in 3
o) c id id id c C31
3-4 0) O O O OJ "4
0 *"4 •> *H *r4 *i-4 fl) (-^ y
•H 01 "4-1 M-I M-I Vl C
43 Vl Vl -H -4 --4 U .* Id
«i4 O C »i4 G C 44 tfl U 4J
Vl Vl C 4-143 & C O> O> C ^ id
oi oi 43 id id vi —4 id "443 •-< id in r-i ai
cn tn tn w QJ o .p Q) QJ oj 0) a) d
O>0)£j>WWflJ(TJO O (0 tO U 03 0
Q O^ Q O* »5 P&4 W &4 O jQ O !2 O tfl Q [2 CQ











01
4J
C
01
^




n\
u*
ft
1— 1

04




(ft
*u
00
n\
U"
o
o








o
r-l fl) 43 C
id o 4J o
3 C -4 73 "4
73 Id 3 0) 4J
•H >i C CO
> 0) 0) -4 D
•-i > 4J 43 43
73 c c s e
C O 01 0 0
H O > O O

01
c u
(fl *H
^
O 01
4J 73
.. 73
C C 0) C
0 (d o o
•^ C CP **^
4J 0) Id C 4J
0) Vl >i"4 0)
3 3 0) 4J 3
J3 4J > CO 43
S ft C -H g
0-
c
01




5*
c
o
0)
~
CQ








1
o





^
o
Vl
Combined and
individual cont
of vents








o*
c
JQ
X)
Vl
u
CO

J.J
Ll
0) Vi
43 01 -4
01 3 id
(d o fl)
2 4-> in
c c c
(fl (0 id
Q4 Ol 04
f* f* f*
•C JC 4?
o u u
id id id .*
0) 0) 0) C
03 CQ CQ 4J












4->
c
0)




o*
c
43
U
id
fit
Ul
ca




73

u
0*
CT>
00

4-1 VI 0
3 U
3 01 01
0« . —
M
•-4 01 a> •• 01
^2 01 Vl 0) Vl 0) 01
olS^S^SSil
noiooiooioioivi
01 73 CUT) CU73 73 ft 01
O
O Vi
73 U 01
C 4J
id <-4 id
id 3
73 3 01
01 73 4-» CO
c -4 m g
-4 > id S
.Q -H 3 0)
S 73 VI
0 C ^ 4J
O -4 0 0)

0)
C U
01 •• Id "4
V) C 4) >
0) O U O 0)
ft-4 -r4 4J 73
ft 01 >
-4 ffl 01 01 C
Vl -H 73 O 0
01 01 i-4 Id C 4J
o >I-H m
§L| Vl 0) 4J 3
•-< 4J > n .Q
01 id C C -H S

CO 3 U U 01 U

01
J3
4J 4J
c
(Q • *W QJ
0) 01 0 73
U Vl C
3 Q) >i 0)
73 £ 4-1 ft
01 ft"4 0)
Vl 01 ^H 73
O •-»
C £ a 73
O ^4J 3 C
~*4 • dj rH (d
4J s O
in ja o) in 01
3 s 43 'H
ja . 4J oi -Q
O 4J O 4J -H
O "4 4J • to
3 C 4J fl
c o c >
. 73 0) 0) •
73 01 ft4-> 01 01 01
§jj O C Q) 01 "4
0 0) Vl 01
3 C >i73 ft i
CO t_^ ^^ C ^^ ^^
tn o ^ 0) tn o
id 0 id ft- 73 '-4
M-I -4 0) CU "4 O
01 4-1 T3 < U C
"4 01 Vl X id 43
Vl id 73 U
>i id ft c o M-I o)
U Id "4 0 4J
C 0) Vi C
01 Vi o 0) id C <-l
•r4 3 1-4 0* 0 O
O 4J 73 J3 Vl -^ Vl
--4 ft 0) Id O 4-1 4-)
<4-l Id 73 "4 O C
•W O O Vl 0) 3 O
0) 0 Id JC 73 U
O<43 > 4J 0)
0) c vi ra
Vl "4 (1) 0) M-I -H
3 Vl Vl -H 0 4J J2
4J -H (d C 4-1
ft 3 >, S 01
id O1 >i O*4J O Vl
U 01 01 O "4 Vl O
Vl 43 ^H rH 0) M-I
4-> 4J O "4 ft •
CO) C 4-1 C 4J
oioiaifidcnoe
OOOlCJi— lO^-^O)
0)3id4J>aiuo)
ft O U O 3 Vi
01 0) ^H 0) "4 73 ft
O J3 0 J= C 0)
O rH Vl 4J Id U 01
i— 1 i-H Q) 4J O^ -
< Vl C 73 Vl 01 O4
oi u (d ox
*> O ^4 *^
0) • -1 01 £ O 01 0
Vl 4-1 U "4 3 CO -4
3 C C J= ~4 C -H C
cao>0)4J730£id
O U 01 -<-• 0) O<
•-( Vl 0) Vl g 4-> Vl
U 0) Vl O U 73 0
C ft-H >w O» 3 C
01 3 C 73 id 01
00 & C --4 0) 43
CnO> 0) O J3 Vl >i4J
c vi -*4 ja u
"4 >i 4-) 3 4-> C iULico>o
•H Id 3 U 01 — t
&tn g 73 oi o o >i
U 01 L| .-4 4J
01 "4 01 Vl 0) 0) M-I "4
Li C 4-1 £ a M-I _l
Id C CD 4-> 0) --I
01 CJ1-4 C 4-> -U
O 0 ft"4 -r4 O< Id  o
373Cca730)O>
o oi o -4 c i e
3 01 0) 0 4-> Vl 43
43 4J tn ft 0) 4-»
4J ft.-l 01 S C 0>
"4 Id S 43 O "4 43 C
5UWE-IUZHO


Id 43 O 73 0)
4-10
-------
 in Chapter 3.0, these controls are currently being applied to
some existing vent streams at most facilities.   (Combustion of
pulping vents in a stand-alone incinerator is possible, but
for this option existing combustion devices were selected.)
Capture is also necessary for those emission points that are
hooded or partially open to the atmosphere (washers,
knotters/screens, and deckers).  As discussed in Chapter 3.0,
complete capture was assumed to be achieved with enclosure of
these points.
     One control option for bleaching vent emission points is
caustic scrubbing which achieves a weighted average of
70 percent reduction for organics and 99 percent reduction for
chlorine.3  A second control option for bleaching vent
emission points is scrubbing the vent stream first, then
ducting the scrubber off-gas to a combustion device.  However,
this control option only achieves an average total HAP
reduction of 75 percent.3  A third control option for
bleaching vent emission points is thermal incineration
followed by caustic scrubbing to achieve 98 percent reduction
for organics and 99 percent reduction for chlorine and
hydrochloric acid.
     The control option for pulping wastewater emission points
is collection of wastewater streams at the point of
generation, handling in an enclosed collection system, and
steam stripping to achieve an 80 to 99 percent organic
reduction.  The overheads from the stripper are assumed to be
conveyed to an existing combustion device.  As discussed in
Chapter 3.0, the design steam stripper control efficiency is
dependent on the volatility of the HAP's present in the
wastewater stream.
4.3  ENVIRONMENTAL IMPACTS
     This section presents the environmental impacts of
applying the control options discussed in Section 4.2 to an
example facility.  These impacts have been revised from the
preliminary draft BID based on internal review, _and address
most, if not all, of the comments provided by industry.  The
                             4-11
-------
example facility selected is a kraft hardwood pulping facility
with batch digestion, rotary vacuum drum washing, and a CEHD
sequence bleach plant (designated in Appendix C as pulping
model PI and bleaching model Bl.)
     Table 4-5 presents a summary of the total uncontrolled
HAP emissions for this mill that pulps 1,000 air-dried tons
per day.  The uncontrolled HAP emissions are presented as
total emissions for the pulping emission points and total
emissions for bleaching emission points, as well as a total
for the entire mill.  In addition to uncontrolled emissions,
baseline HAP emissions are presented in Table 4-5.  These
baseline emissions were estimated assuming that its digester
relief, blow gases, and evaporator noncondensibles are
combusted.  No other baseline controls were assumed for this
example.  As discussed in Section 4.1, in estimating national
emissions and control impacts, baseline control levels were
considered in a plant-specific analysis.
     This section presents the environmental impacts for
application of the previously defined control options on this
example mill.  Section 4.3.1 presents the primary and
secondary air impacts of these control options.  Section 4.3.2
presents the energy impacts.  Water impacts and other impacts
are described in Sections 4.3.3 and 4.3.4, respectively.
4.3.1  Air Impacts
     This section presents the primary and secondary air
impacts resulting from the application of all control options,
discussed in Section 4.2, on the example pulp mill.  Primary
air impacts include the reduction of HAP, VOC and TRS
emissions directly attributed to the control option. Secondary
air impacts evaluated are the increased criteria pollutant
emissions resulting from steam generation for steam stripping,
from auxiliary fuel combusted in the incinerator, and from
combustion of vent streams.4
     Table 4-6 presents primary air impacts for the example
mill, by control option  (as presented-in Section 4.2).  The
                             4-12
-------









id
>*
H
H
r3
H
0
<


H
ij
PU
jg
H

3
0
PH

CO
8
o
H
CQ
CO
H
22
W
a
H
ij
o
Pi

55
0
O

5


•
m
i
^»

H
^3
S
EH












CO
Cc ^^
o *^^
, Q^ «rH J/^
w ffi.2 ^
n) s S
MP3 s^-»
0)


TJ g
0) §
rH O
. rH "Jj .— x
rij O *M V-l
t* o ® sT
0 fc —

3 2
MH

1,
TJ o
Q) ]j
rH 0-°
o us *->
i 
u c
W -H
(0 ^ Q)
O M XJ
TJ -P O
C O -P Q)
rtJ (0 O ^
i C
03 --.
(0 ^» CO U
> rH >, >, O
(0 nj to 4J
^"i J'J TJ TJ (0
rJ 0 -*. rH
- >
m a)
C TJ *
O CO  (0 O (0
c — 'H en
XJ -H -*.

•P O r^ 4J S O
(0 (0 1 -H — rH
X» a) •* o X)
rH 0} *
X! X) TJ Ou TJ
+j c a — c
•H TJ (0 O CO «J
5 C C
fC CM II O <1H
tji i 4j a) •
C O* ^* *"^» *H (U
•H C rH «H rH C
CX -H CQ >i « Q) -H
rH Clj Q) "-.H VH rH
3 rH rH CT> 	 Q)
a 3 xj g tn ^ co
TJ &H ^-^^> X>
O <4H CO * W
O O C C ~ Q) 4J
> -H O Q< OT> <0
TJ C -H rH -H
>H O TJ CO 3 TJ TJ
(0 -H CD co a. a)
£ 4J *J -H CO 4J
• -H C g &» Q) W
.p-pcawsgd
-------
^^
w
^
§£
•H
(OX)
CO C
•H O
g *H
O
3
TJ
CU
03
C
O
4J
o
3
0) ^
c ^
o
-J
•o
CO
CO
•H
n
w
03

U
o


cm

HH


w
03
EH


U
O


OH
(2

c
o
s
o

o
M
^
o
u
co
c
o
•H
CO
co (0
•H ^
1 — .
•H "- •
0)
CO
(0
CQ

w
03
EH


U

ft
<
X
C
O 0)
•H O 0)
to JH a
W 3 >i
•H O EH
g W
w

o
(N
in
o
o
H

O
in
H


TJ
o\o
CO
Cn

TJ
0\»
CO


TJo
CO
en
TJ
"'o
C C
O O
•H -H
4J 4J
O 10
0) 3
"H A
•H g
0 0
U 0

o

in


o
vo
H
H

O
VO
H

•H CO
a-P
rH C
3 0)


§

O
OI


o
CO
n


<


0\«
0
[^


tl 1
o\<>
O
f»

0)
c
•H
3
O
w


o



o

o
in
in
>T>
leachinc
ents
fD >
O
H
O

in
oV»
CO
oV

Cn
 I
CO
 c c
 0-H
•H rP
4J XI
 (0 3

 0) O
 c co
•H
 O TJ
 C C
         o
         m
         OJ
         o
         o
         o
         co
         o
         H
         0\»
         oV>
         o
             a

         (0 -H
         CD  M
         4J 4J
         CO  CO
         O
         O
         n
         o
         o
         irH
                             •  C X
                           >i O W
                           O 4J U

                           (Don)
                        (d *H o
                        CP O O TJ
 CO
 0)
 CO
                        8
                        (0 O  CU CQ
                        cu a. (0
                        CU
                           CO
           g
           3
                                o  (0  >
•H -H <)H

          TJ?  C *
              O
                                         OJ
                                         O
                                         r4
                         CQ
                         C
                         O
                  O  CU  H
                                         *  O •—
                                            i
               CU


               CQ
                                3
                               TJ
              •H
               CQ
               CO
              •H
               g
               O
                                                       (0
•H  *
 (O
•H flj -H
 (0 0) 4->
    >i-H
                               CU C     O O  0> (0
                        CQ
                        C
                        o
                               0)
                            en c
                            c  o
                               o
                        CO
                        CQ
                       •H XJ
                        g-H
                        CU  CQ
                            C
                        CU  CU
                        C TJ
                                  •H  C iH  H
                                  4J  O
                                  CO-H  ||
                                  CU 4J
           x:     &»
           q  EPS
           4->  C  ^
           (O-H
               o  c
           X! H  0
                              <
                                                             rH>
                               
              jQ  O
               3  C
               M  RJ
               o  x:

                  0)
               cu  g
               !H
               (0  «V>
                  O
               co  r»
               cu
                             co  x


                             3  en
                             O  T!^
                            ^j

                            rH  aT

                             (0  -H
                                >H
                             g  O
                             O  rH
                                                                     r4 cW>
                                                                     O CO
                                                                     4-> 
                                                                     (0
                             CQ  o\«
                            4J  CT>
                                >i  Q)
 CQ  4J

 O  g
•H  (0
 co  o
 0)  O
    o

 O  CQ
                               C  3  O  ^4  (0
                               O  O  (0  O  Q)  CO
                               -H  >H  rH     CO  (0
                               4J X>  XJ TJ
                               CO         0)  TJ  C
 O1 O
•H -H
•H  C
    «J
    CQ

 C  O
 (0 rH
4J rH
    O
                                                              xiMnJ3
                                                                            (0 -H
                                                                               4J
                      o  co     ra  M  3
                         (0 TJ  O  0)  TJ
                     TJ  3  c     x:  Q)
                      c      n)  co  CQ  M
                                       TJ

                                       flj
                                                                                       CU
                                                                                      •H
                                                                                       O
                  O

                  (0

                  CO
                  0)



                  CO
                                              3
                                              O
                                              14-1
                                                                                       (0
                  co
                  4J

                  (U
 C
 (0
4J
                                              (0
                                              CU
                                              CQ

                                              TJ
                                       CU
                                       x:
                                       CO
                                       (0
                                       3
                      CU  O  CO  3     C
                      >H  -P  C  TJ   --H   .   *
                      3CQCUCU>HCOOHr4
                                                              & 3 r4     3 -H
                                                              m  O O  C O  g
                                                              O  r4 CQ  O 4J  CU
                                                                 XI ^.-H
                                                              (Q     CQ 4J CO 4J
                                          X  3
                                              o
                                           r4  4J
                                           cu
                                     •  o
                                   TJ  
                            0) O
                            4-> en
                            CO

                            cu of
                            IH 03
                      CQ o\«

                     4-> en
                      rt)
                      CO   -

                      cu w
                     TJ S

                      O 0\°
                                                     CO rH

                                                     CO  O  rH
•H 4J 4->
 U (13  0)

    O
 en
 C cu
 O
•H TJ  CO
4J C  3
 O (0  O
 3    rH
TJ CO rH
 CU CU  O

    (0
o\o CQ  CO
en
en
                                                  C  (0
                                                  cu
                                CO  C O
                                O  O-H

                                c     o
                                (033
                                0> O TJ

                                O X5 M
                                              O  CU O
                                                 4J -H
                                              C  CO CO
                                              O  CU CO
                                              •H  OVH
                                              4J-H g   •
                                              O TJ CU Oi
                                              3
                                          x: co  cu TJ  CQ 4J x
                                COCU3CU^XJ3O      33     3  O  Q)

                                g(l)COnJCUOCQCUOCOOcocQO4J
                                                              O
                                                TJ (1) M-l     D<    £ -H -r-i
                             4-14
-------
table presents uncontrolled and baseline emissions of HAP, VOC
and TRS from pulping vents, bleaching vents and pulping
wastewater.  Estimated emission reductions for the different
control options were calculated for these vent and wastewater
streams and are presented in Table 4-6.  For the control
options selected, the pollutant removal efficiencies vary from
70 to 99 percent for total HAP, total VOC, and TRS, as shown
in the table.
     Table 4-7 presents secondary air pollution impacts for
the same example mill.4  As shown in Table 4-7, the greatest
secondary impacts occur from the generation of steam used in
steam stripping the pulping wastewater streams.  Annual
impacts of 63 Mg/yr sulfur dioxide, 172 Mg/yr carbon, monoxide,
and 123 Mg/yr nitrogen oxides were estimated to be generated
from steam production for this option.4  The secondary impacts
were estimated based on calculating the amount of fuel
required to generate the steam and the increase in criteria
pollutants based on literature values.4/5
     The impacts associated with combustion of pulping vents,
including steam stripper overheads, were determined to be
negligible (with the exception of sulfur dioxide from the
combustion of TRS in the vent streams).  All HVLC vent streams
were assumed to be" used as combustion air for existing on-site
combustion devices, with no significant effect on the fuel
usage requirements, while LVHC vent streams were assumed to be
used as auxiliary fuel.4  The sulfur dioxide impact was
estimated based on the amount of total reduced sulfur in the
vents requiring control.  Although the additional moisture
added to the combustion device will result in additional fuel
requirements, the addition of organics to these combustion
devices from the vent streams offsets the associated fuel
requirements.6
     Scrubbing bleach plant vent streams was assumed to have
no impact on secondary air emissions; however, incineration
followed by scrubbing of these vent streams will result in
secondary air pollution impacts, resulting from the combustion
                             4-15
-------














w
1

!
H
a
o
H

a

!_q
o
CU

0$
H
14*

X
1

o
o
H
CO

j
1
H


U
J
P
M
J3
£2
H


^
pa
0

g^


























O
*
,Q
•j;
>.,
fr
s
^^
(0
c
o
•H
CO
w
•H
g
w












Tl

o
g
v*^





^
o






o
u







(N
o
CO





g
(A4







fl
c
o
•H
4J
a
o

rH
O
4->
C
O
U




(U
f\
t.
M
o
CQ ..
WJ d)
C« tr^
O r^1
•H "

U
•H
fl





o








o






o







^^
^0






o












73
c
(0
Q)
G G
O 0
•H -H
[ \ i\
O W
0) 3
rH X!
rH g
O 0
U U





CO
4J
c
O


O"1
c
•H
a
rH
3
Ol




0 O 0







o ,_.
OH °






° S «







-_ ^N
0 ' M
O N





0 ^ "
H









^ 0^
C CP
<0 C
•H
c PI
O p|
•i-( <4-| -H
C flJ C 4J
•rH >4 -H CO
X! Q) XI
XI C X) g
3 -H 3 (0
M 0 to Q)
0 C 0 4J
CO H CO CO



W
4J
c
V
^
QPl Q)
C 4J
•H 0^ (Q
X! C >
O -H Q)
(0 Q^ ^J
^
rH
4J
•H
O
•H
i— 1
p.
X
0)

-a
0)
c
•H
M-4
(U
T3

<0

(0

73
0)
i— i
rH
O
J_,
4J

0
O

O1
c •
•H T)*
0)
XI 0)
o
10 C
0) 0)
O M
^ 0)
3 ^4«J
o a)
(0 PS



«3 Xt



xt
o
fT5
4-) 0)
U-4 rH
n) Xt
^
y Q
rn
J>i H
rt) U
T3
CO
G ""O
0 C
4-1 (8

O ^P
0 G
0 -H
* X!
rH !/}
(0
0) 3
rH
a g
g 3

X T3
a)

C VH
(0 (0
^i
r4 O
O M
0
T3 C
0) O
4J-H
(0 4->
rH W
3 
O O»
rH -H
(0 T3
O

CO O
G 4->
O (0
•H XI
CO
Ul JZ
•H 4J
0) 3
4-> rH
C rH
03 -H
4J g
3
rH a
i-H rH
O 3
Pi pt

-SI
r4 O
Q) ^
4J T3
•H r-l
r-l (C
0 X!



0
""O *O Q
Q) 0)
rH 4J g
•H 3 OH
O O a)
>H >H  0 4-» XI
C W Cn OHO
0 4J C C C 4J T3
U C-H 0 C
0) > -H 01 • T3 (0
4-> > Q) 4-> g CO (U
O -H O (0 (1) g G
COX! 3 3O
i-3 O 73 J-i nj Ul -H
W > (0 (U 4JU1U14J
4J 33 In W C (0 0
C to (1) 3
>rHXt O 0) C 0) Q)
C 4-IX104-) <1J
MC 4-» O O O O
CO (0 O CO CO O44-I CO
« AJ a a «3

nl 4-> >i O Q) 0) C
 -H C  t04JOT33O
g rH G O VH
C (0 'O O ^ C ^0 J^ Q)
• O O Q) ^ Ul O Oi
Ul-H^a OQJ-H30)
 & CrH4->Or4O
o fO M *H Cn (0 rH (0 ^
•Hr4(U3 ••Hftfr-lXt
>0)X!O1C 0) U10>

73 -H RJ -H (U (0 -H QJ (0 -H C
U 3 <1> 4-> 4-> O 4->  O
rH C Xl O (0 VH C W XI Q) *H
O -H 73 3 M 3 -H 0) to -H 4->
rH CO73 O O»0)X1O

CO rHOOO73OtOT3
O >H 4-> 73 *H to (U
U> 3 O-H cnffiOCO
O3U1^4gC(d3COCOCQ *H
^S^rH^^^W^gfll
rH -H CN 3 r-l (0
73 OOrHtO 4-IOJX1S
0) CM"XlCOrHC (N (0 -P 4-1 &|
4JOQ) OOO W-H
(d CO C rH 4J CVH CO 73 3 4J
M-HQ)C Ul 0)O^C
3-Ha
«JOO -HrMOCt03
rHOC4JOOrHOCO H (0 4-> (T» U CO H 0 to d) O



73 Q) 
-------
of these gases in a stand-alone incinerator.  In addition,
secondary air impacts from the combustion of auxiliary fuel is
included.
     Figure 4-1 graphically presents the primary and secondary
of these gases in a stand-alone incinerator.  In addition,
secondary air impacts from the combustion of auxiliary fuel is
included,  air pollution impacts shown in Tables 4-6 and 4-7
for this example mill.  The combined impacts for ther control
options for pulping and bleaching vents and pulping wastewater
are shown in the figure.  The control option selected for
bleaching vents depicted in Figure 4-1 is scrubbing only
(i.e., the impact for incineration followed by scrubbing is
not shown).
4.3.2  Energy Impacts
     The control options evaluated require additional energy
in the form of electricity to operate fans and pumps,  and
additional fuel to generate steam and to combust bleach plant
vents.  Table 4-8 presents these energy impacts for the
example mill, broken down by pulping vents, bleaching vents,
and pulping wastewater control options.4  As stated
previously, no additional fuel requirement was assumed for
combustion of pulping vent streams; however, additional energy
will be required to transport the vent streams from ^the point
to the combustion device.
     The amount of electricity required to operate the fan or
blower is estimated by calculating the horsepower required to
transport the vent stream.  Electricity to operate fans and
pumps for operating scrubbers and steam strippers was
calculated in a similar manner.  When an incinerator is used
to control HAP emissions from bleach vents, auxiliary fuel is
required to sustain combustion.  The auxiliary fuel was
estimated based on the combustion temperature, VOC content of
the stream, and volumetric flow rate.  When a steam stripper
is used,  auxiliary fuel is required for the generation of the
steam.  The fuel requirement was estimated based on the steam
requirements.
                             4-17
-------
                                                                        ALH99l8ZZi
o
s
CM
                                                              If
                                                              si
                                                              "I
                                                               II
                                                               2
                                                               i
o
n
n
  f
J§
                                                                   a.
                                                                   <
  O
  (0
  a



  c
  o
                                                                             o
                                                                             a.
                                                                             a.

                                                                             £
                                                                             (0
                                                                             x
                                                                             £
                                                                             13
                                                                             O)
                                        suoissjug
                                      4-18
-------











J3
Rt
to
MPACTi
H
X
O

pq
2;
U

J
H
5J

H
,j

M
*3
3
u


,
eo
«i
TABLE -

















rH
(0
4J
O


TJ
W
0) _.
^83!
3f{*S3
X * rl "g §
3«£ss
*• 3 ^ cn-~
i  £
2-H . *
3g«3
•H (2 ^ m
X ^ 3 S '
3 -P B
< 
^ _TJ
•P /«
o a
CU g

W ""



o
c
0
Control Opti



CU

c ^
O r.
•H ^
m «
w o
•H £
o
CO



.0
o

n





g





1





o
o
^
n










T3
Collection ar




.p

cu


^n
c
•H
cu
rH
3
CU





































Combustion















0
0
in
en





g





1





o
o
in
^
cr»











Scrubbing


.p
c
0)


C7^
C
•rl
o
«S
0)
rH
CO

O
O
O
O
VO
O
i-l





g




0
o
o
o
in
o
»
H



O
O
in
^
cr>









C
(0
Incineration



















































Scrubbing















o
o
o
^
n
a\
01




o
o
0
o
01





z





o
o
0
^
n









&
C
Steam Strippi






j_i
cu
4J

C S
•H CU
rH 01
3 «J





4J
3
rH
rH
•rl
e

a
rH
3,
•a
0 •
O 4J
3 C
T3 (0
rl rH











(0 CU
x;
-P O
VM n)
n) CU
rl rH
y Q
(0 S3
•O W
"c"
O (0
-p
T3
0 C
O (0
o
H C
•H
CU £.
rH W
04 (0
6 3
fl
x e
CU 3

C *O
(0
rl 3
O 3
calculated f
n, rotary vac
(f] O
-P-H
• O -P
•«* (0 W
Cu CU
cu g o*
O -H -H
C T3
CU >i
j^ ^n jC
CU It O

rH
4J
•H
O
•H
rH



cu
CO
cu
•*•*
c
•H

•H
c
o
•H
10
3
XI
e
o
o
-p
Q)
•H
X)
(C

CU
^
. 0
Q
5.
CU
Sj
CU 3
X
cu

TJ
CU
C

M-l
QJ
T3
CU
controlled ar

C7
C
•H
CU
xt

U)
cu
u
rl
3
O
CO


0
jj
io
•r|
O
g

CU

-p

o
1 required fr
cu
• 3


rH
(0
C
o
•H
^J
•H
•o
a


•o












•
(0
itream
VI
+J
C
CU
>

cu
X!
.p
O

0)
3
rH
(0


rH
CU
3
<4_|
CU
X!
+J
Xt
4J
0)
W •
 2



4-19
-------
     The greatest impacts are incurred with incineration and
scrubbing of bleaching vents, representing approximately
1.1 x 1012 Btu/year for the example mill.   The next largest
energy impact results from the generation of steam, used in
steam stripping pulping wastewater streams; however, this fuel
requirement is less than the fuel requirement for incineration
of bleach plant vent streams.
4.3.3  Water Impacts
     The water impacts associated with the control options
discussed in this section are being evaluated quantitatively
by EPA's Office of Water as part of the joint rulemaking
effort, however, this section presents a qualitative
discussion of the potential water impacts associated with
these control options.
     Control of pulping vents through collection and
combustion in an existing combustion device was determined to
have no impact on water pollution.  Any condensates in the
vent stream collection system can be returned to the weak
black liquor recovery system or to the condensate steam
strippers.  Scrubbing of bleach plant vent streams will
contribute approximately 1.5 pounds of sodium chloride to the
wastewater (5 to 40 ppmw); however, this quantity is small
compared to baseline total dissolved solids quantities.7
Steam stripping of pulping wastewater streams will positively
effect the quality of the pulp mill effluent, specifically
methanol loading reductions.  Lower methanol loadings will,
consequently, reduce the biological oxygen demand loading.
4.3.4  Other Impacts
     Other impacts considered for the control options
discussed in this section include noise, visual impacts, odor
impacts, solid waste impacts, and irreversible and
irretrievable commitment of resources.  Although some of the
add-on control equipment will" increase the noise level in a
pulp mill, the incremental noise increase will be small
compared to background levels.  The increased noise levels

                              4-20
-------
will occur from fans and pumps used to transport the vent
streams and wastewater streams to the control devices.  No
visual impacts associated with the control options, however, a
positive odor impact will result from the additional reduction
in the malodorous total reduced sulfur compounds emissions.
No expected secondary solid waste impacts associated with the
control options discussed in this section.  Any waste
generated from steam strippers or scrubbers should be
manageable within the existing waste treatment process.  No
significant increase in incinerator ash is expected.  No
irreversible or irretrievable commitments of resources
associated with these control options have been identified.
                             4-21
-------
4.4  REFERENCES


1.    Memorandum from Olsen, T.R., and P.B. Murphy, Radian
     Corporation, to Lassiter, P.E.,  EPA/CPB.  Database
     development and model approach.  January 27, 1992.

2.    Memorandum for Olsen, T.R., Radian Corporation, to Shedd,
     S.A., EPA/CPB.  Revised Model Process Units for the Pulp
     and Paper NESHAP.  September 21, 1993

3.    Memorandum from Olsen, T.R., Radian Corporation, to
     Shedd, S.A., EPA/CPB.  Model Scrubber Removal
     Efficiencies.  September 17, 1993.

4.    Memorandum from Bagley, C.J., Radian Corporation, to
     Shedd, S.A., EPA/CPB.  Secondary Impacts.
     September 24, 1993.

5.    Compilation of Air Pollutant Emission Factors.  Volume I,
     Stationary Point and Area Sources.  Fourth Edition.
     U.S. Environmental Protection Agency, Office of Air
     Quality Planning and Standards.  Research Triangle Park,
     NC.  Publication No. EPA/AP-42.  Section 10.0.
     October 1986.

6.    Memorandum from Greene, D.B., Radian Corporation, to
     Project File.  Fuel Penalty.  October 8, 1993.
                                        c
7.    Memorandum from Olsen, T.R., Radian Corporation, to
     Shedd, S.A., EPA/CPB.  Pulp and Paper NESHAP Selection of
     Bleach Plant Scrubber Design and Costs.  October 8, 1993.
                              4-22
-------
                  5.0 ESTIMATED CONTROL COSTS

     This chapter presents the approach taken to estimate the
cost of controlling hazardous air pollutant  (HAP) and volatile
organic compound (VOC) emissions from the pulp industry as
discussed in Chapters 2.0, 3.0, and 4.0.  This chapter
discusses the assumptions used for sizing the control
technologies for each emission point, the method of estimating
costs for control technologies (Section 5.1), and the
estimated costs for an example facility (Section 5.2~).
Table 5-1 presents a summary of the elements included
(enclosures, combustion devices, scrubbers, and steam
strippers) in the control cost analysis for the emission
points identified in previous chapters.
5.1  CONTROL COSTS
     This section presents the methodologies used to determine
the cost of controlling vent and wastewater emission points in
model mills that are used to represent the pulp industry.  The
approach used to size and cost the control technologies was
                                                              •
dictated by the EPA OAQPS Control Cost Manual (OCCM).   This
manual uses conservative estimates of design parameters where
specific industry data are not available;  thus,  resulting cost
estimates can be conservative (high).  Consequently,
significant changes in costs are not expected,  and therefore,
decisions made based on these preliminary analyses are valid.
Sections 5.1.1 and 5.1.2 discuss costs for enclosures and vent
gas conveyance systems.  The control technology costs,
including thermal incineration, scrubbing, and steam
stripping, are discussed in Sections 5.1.3, 5.1.4, and 5.1.5.
In each section, design assumptions,  design parameters
affecting costs, as well asestimated costs are presented.
                              5-1
-------














o
H
EH
"(
H^
^3
U

j<
c5

EH
W
O
O M
W
tJ U
Oi_i
• I
EH W
2 Q
O "••«•.
U CO
EH
a 2
H H
o
Q (^
Q cn
D D
i-3 O
O H
\s rn
23 ffi
M >
w
EH 05
a o
W frt
Sit
fyl
.1
HH



9


1
tn

w

(X)
f3$
EH

















u
c CD
0) ft
•P "4
W Ll
4J
m




JQ

0)

3

U
w



c
Old
•H 01
4J 0)
01 U
3 "4
X! >
S OJ
o-o


^*s* ^
|J U
°!
*S
o 2
3
Q °


Q)
D
g
01
0
Q
H












•P
C
•*H
a

c
o
•t-l
01
01
"H
c
w













x ~












XXX






*

XXXXXXXX X X XXXX






XXXXXXXX X X XXXX









XXX





5
Q
0) -H
D^ jQ
id
Ll C C
O O O TJ
4J — 1 — I 01
01 01 U JJ 4J £
id fl) id id id
O> 01 Ll U U 0)
Id .* 0 -H -4 Ll
IW Cn 01 C 4J 3 *4-4 *W 01 -P
0) c -l LlLig •-( --I p ffl 4J > (1)
LI ja oiuiaLiJ< >-t >HC vc ±>
£ 05 O O U 4J 0) 0)0)01CO)^id
Ll Ll 01 01 ^«* M-4 4J Id C *O *O ^ -P 0) ^ C 3
01 o) o) LI id 01 id f^ Q c ^ id 0)
JJ4J4JO)3L|L|L| .Q ^C CLlO) LI4J4J
C01014J 0) 0) O 0) Q) 0) > Ll Q) 01
0) 0) Q) -P ft »-^ «c ft ••'tf J^ cn^ Cn i£ 0) «c *H id
g> encno^H u 01 id idc ^iC ^ico o 3 01 id 3
OQQ»^CUQSUi2'PO4JO3"^EH^O D
C £ C -
~( O "4
O id o
-l
3 -I 3
a, 00-0.
-
01
0) Ll
O ft rH
~* ft O
id -H LI
1 Ll 4J
•O JJ C
C 01 0
id u

01 id >i
01 Ll
«. 4j id
Ll 01 S
01 "4
> Ll Ll 0)
01 01 ft U
3 -^ *^
O id 0) >
.C 3 -C 0)
01 -P -a
••*. ^J
0) 01 01 C
•-t id id o
j2 3 **H
id 4J
U 0) •• 01
••4 .C 0) 3
^H -P C A
ft o e
ft S -H 0
id o -P • o
M Ql ^J
0) m o 0) O>
J2 ft C
01 rH ft-H
o id o -H -P
-P Cn • LI LI 01
Q) 4J 4J "H
•a -P o c 01 x
0) C -<-l 0 • 0)
e 01 > o c g
3 > 01 O id C
01 "O 0 -H ai id
01 0) 3 -P JJ
id £ c -p id 01 o
HO Ll 4J
0) -H C Q) 0
Ll .p -^ C 4J T3
0) • 01 -H 01
3 01 3 01 O Ll >.
•P XI -P C 01 0)
01 C E C -1 .p >
ai ai o a) id c
o > o > en 3 o
•*H C 0) O
> en en 4J --4 v
01 C C C 3 01 0)
•O --4 "4 Id O id Ll
J3 4J rH .H 3 Id
C U 01 ft^H
O Id "4 O «-i 0 0)
*J ^H 0) O ft
01 J3 Id ^ 4J ft
3 C 0) O Ll -^
XI Ll Id i-l Ll 0 Ll
£O XI .p ft 4-1
O i4J 0)
••H a> -P "a LI 4J
4J "O 01 0) id "O 01
m -H 3 LI -o c
••H o) xi ai c id ai
x c e T> o f
01 O O •* O C 4J
U U 01 0) 0
- C 01 -H g
01 fl) Q) O 4J 0
+J Ll XI O id O Ll
CO) 0) H-i
Q) 3 0 01 0) n-t
> 4J LI id -H a
0) 0) 0 TJ
Cn LI T3 3 *O O id
C O 01 C 0)
•^ .p g 01 id cnj3
tt id 3 Ll C Ll
<-4 Ll 01 01 •-•* 10
3 01 CD XI 01 T3 >
a c id ja u 3 o
-^ 3 -^ ^
Ll O 01 Ll > O 01
O C id U Q) C .C
Cn -^ 3 W "O M H


id xi o -o
5-2
-------
5.1.1  Enclosure Costs
     As shown in Table 5-1, the emission points that will
require enclosures before an end-of-pipe control device can be
used are the pulp washers, the knotters, and the
screens/deckers.  Enclosing these points reduces the
volumetric flow rate typically associated with capture of the
emissions and will increase the overall capture of VOC and
HAP.  Factors considered in estimating enclosure costs include
the size of the enclosure, the materials of construction, and
the need for equipment access.  It should be noted that some
washer designs, such as diffusion washers, do not require
enclosures due to their design.
      The costs for enclosing the systems (model washers,
etc.) were developed based on vendor quotes for enclosures
installed on pulp washers.1  The enclosures are assumed to be
a close-fitting panel hood design.  Vendor cost quotes were
obtained for enclosures constructed of fiber reinforced
plastic (FRP) and designed to allow equipment access.  An
approximate purchased equipment cost of $40,000 was assumed
for each enclosure at a typical (i.e., 1000 ton per day)  mill.
Additional supports are required for the close-fitting panel
hood when designed for a rotary vacuum pulp washer to support
the weight of the hood and to provide structural support for
access openings.  A washer line consisting of three rotary
vacuum washer drums was assumed to require three enclosures,
with two additional supports at $12,000 per set.1  It was
assumed that screens, knotters, and deckers each exist as
single units, and require a single enclosure.  For mills with
larger capacities, it was assumed that multiple lines/units
would be used and would require additional enclosures.
     Direct and indirect installation costs were assumed to be
50 percent of the purchased equipment costs; therefore, the
total capital investment was estimated to be 150 percent of
the purchased equipment cost.  The resulting total capital
investment for enclosures in 4th Quarter 1991 dollars is
approximately $64,000 for each screen, knotter and decker, and
                              5-3
-------
$230,000 for washers.  The costs were annualized assuming a 10
year equipment life at 10 percent interest rate.  The
resulting total annual costs (TAG) equal $10,400 for each
screen, decker, and knotter and $37,500 for washers.
5.1.2  Ductwork and Conveyance Costs
     Ductwork is used for the conveyance of vent streams from
discrete points or from enclosures to the control devices
discussed in Chapter 3.0.  It was assumed that the mill would
combine vent streams and send them through a single duct to
the control device; therefore,  the ductwork system was sized
to allow multiple emission points from a process area (i.e.,
knotter and pulp washers) to be routed together to be conveyed
through a common ductwork system.
     5.1.2.1  Ductwork Design Considerations Affecting Cost.
The ductwork system consists of the following equipment:
ductwork and elbows, fan, knock-out drum(s), flame
arrestor(s), rupture discs, supports, and insulation.  Table
5-2 presents the assumptions used to calculate ductwork costs
for venting pulping streams to an existing combustion device.
     A minimum duct diameter of 8 inches was chosen to
represent the smallest reasonable duct diameter from low-flow
points.  The main header diameter was based on the cumulative
stream flow rate and an assumed maximum velocity through the
duct (3,000 feet per minute) for combined vent streams.2/3
The duct was assumed to have an overall length of 1,000 feet
from the emission points to the combustion device based on
site visits and mill teleconferences.  For the flue gas from
the combustion device to the scrubber, the overall duct length
was assumed to be 300 feet, and for bleach plant emission
points to a stand-alone scrubber, the overall duct length was
assumed to be 100 feet.  For this preliminary analysis, it was
assumed that the cost of a large, constant diameter duct would
approximate actual costs incurred by scaling up duct diameters
with transition pieces.  A comparison of these assumptions for
a model mill is discussed in a separate memorandum.2
                              5-4
-------
    TABLE 5-2.
DUCTWORK GENERAL DESIGN SPECIFICATIONS FOR
VENTING TO AN EXISTING COMBUSTION DEVICE
              Item
                  Specification
Design and
   Cost
references
 Minimum duct diameter

 Target pressure drop


 Maximum duct velocity
                    8 inchesa

                 20 to 40 inches
                     of water

                 3,000 feet per
                     minute
     2


     3
Duct length
Number of elbows per 100 feet
of duct
Fans per duct
Flame arrestor per duct
Knockout drum per duct
Number of rupture discs per
100 feet of duct
Thickness of steel
1,000 feet3
23
1
1
1
1
16 gauge
2
2
2,5
6
2
7
4
a  Based on site visits to several mills.
                              5-5
-------
     5.1.2.2  Development of Ductwork Capital Costs.   Duct-and
elbow cost equations were developed for carbon steel  and
adjusted to reflect the cost difference of stainless
steel.2/4 Additional costs were included for the fan",
supports, insulation, knockout drum(s), flame arrestor(s), and
rupture discs.5/6/7/8  For bleaching vents controlled by
an incinerator followed by a scrubber, a quench chamber is
used to cool the stream.  The halogenated streams from the
combustion device are conveyed to the quench chamber by
stainless steel ducts.  After the incinerator gases are cooled
by the quench chamber, FRP duct is used to convey the gases to
the scrubber.  To determine costs, an FRP multiplier is used
in place of the stainless steel multiplier.  The total capital
investment was estimated as 3.02 times the sum of the
individual purchased equipment costs to account for direct and
indirect installation costs, including retrofit costs.9/10
     5.1.2.3  Development of Ductwork System Annual Cost.
Annual costs for the ductwork system include utility and
maintenance costs, as well as annualized capital charges.  It
was assumed that an  increase in operating labor due to the
ductwork is insignificant.
     Electricity is  the only utility cost considered.  The
electricity requirement for the fan was calculated from the
vent gas flow rate and the estimated pressure drop through the
duct system and a cost of electricity of $0.04 per kilowatt-hr
($0.04/kW-hr) .11
     Maintenance material and labor are included under
maintenance costs.   Maintenance labor requirements are assumed
to be 0.5 hour of labor per 8-hour shift.  Maintenance
material costs are assumed to be equal to maintenance labor
costs.12
     The annualized  capital charges include  capital  recovery
charges as well as taxes, insurance, administrative, and
overhead charges.  The capital recovery cost assumes a 10-year
duct life and 10 percent  interest rates, and is calculated
using the following  equation:
                              5-6
-------
 Capital recovery  Total capital   Capital recovery
                  =  .     4.   j.  *      ^           (10 years,  10%)
       cost          investment         factor

Taxes, insurance, and administrative costs are assumed to be
4 percent of the total capital investment.  Overhead is
conservatively estimated to be 60 percent of the total labor
and maintenance costs.12
5.1.3  Thermal Incineration System Costs
     Thermal incinerator costs were developed using the cost
equations presented in Chapter 3.0 of the OCCM.13  As
discussed in Chapters 3.0 and 4.0 of this document, a thermal
incinerator may be used to control HAP and VOC emissions from
halogenated bleaching vent streams.  Thermal incinerators may
also be used to control pulping vent streams if desired;
however, for this analysis it was assumed that pulping vent
streams would be controlled by an existing combustion device.
Costs for a thermal incinerator for an example bleaching
process are given in Section 5.2, and the design consideration
for halogenated streams are given below.
     5.1.3.1  Thermal Incinerator Design Considerations
Affecting Costs.  The thermal incinerator system for
halogenated streams consists of the following equipment:
combustion chamber, instrumentation, blower, collection fan,-
ductwork, and stack.   The OCCM contains further discussion of
incinerator control system design.13  General thermal
incinerator design parameters are presented in Table 5-3.
Other key variables that affect costs are:  vent stream flow
rate and type of heat recovery (capital costs)  and vent stream
flow rate, vent stream heat content, and fuel requirements
(annual costs).
     The amount of oxygen in the vent stream or bound in the
VOC establishes the supplemental combustion air requirement.
In pulp mills (including pulping and bleaching vents), most of
the vent streams are dilute streams and contain an oxygen
percentage sufficient to support combustion.14   Therefore,

                              5-7
-------
 TABLE 5-3.
THERMAL INCINERATOR GENERAL DESIGN SPECIFICATIONS
        FOR HALOGENATED VENT STREAMS
              Item
                            Specification
 Emission control efficiency

 Minimum incinerator capacity3
 Maximum incinerator capacity
 Incinerator temperature
 Chamber residence times
 Supplemental fuel requirement
                   98 percent or greater
                   destruction of VOC
                   500 scfm
                   50,000 scfm
                   1,100 °C  (2,000 °F)
                   1.00 sec
                   Natural gas required to
                   maintain  incinerator
                   temperature
a  Five hundred scfm is the minimum incinerator size used to
   determine capital cost.
                              5-8
-------
for pulp mill vent streams, supplemental combustion air is not
expected to be required.  In fact, certain pulping vent gases,
such as digester relief and blow gases, may have heat contents
greater than approximately 100 Btu/scf due to the presence of
turpentine compounds.  In such cases, the vent stream may be
used as supplemental fuel in combustion devices.15  (See
Chapter 3.0 for discussions on vent streams and their heat
contents.)
     The minimum and maximum incinerator flow rate for this
cost analysis were 500 and 50,000 scfm, respectively.   Flow
rates greater than 50,000 scfm were assumed to be controlled
by multiple incinerators.
     Halogenated vent streams were not considered to be
candidates for heat recovery systems and were costed assuming
zero percent heat recovery.  This design assumption was
imposed because of the potential for corrosion in the heat
exchanger and incinerator.  Based on an analysis of chlorine,
chlorine dioxide, extraction, and hypochlorite bleach plant
stages, vent streams that would likely contain higher
concentrations of halogens would be from the hypochlorite
stage (chloroform) and the chlorination stage (chlorine).  If
the temperature of the flue gas leaving the heat exchanger
were to drop below the acid dew point temperature for these
vent streams, acid gases would condense.  In cases such as
bleaching vents steams where heat is not recovered, the annual
fuel costs would be higher than for cases where heat recovery
is practiced, other factors being held constant.
     The destruction of VOC's is a function of incinerator
temperature, residence time in the combustion chamber, and
concentration of VOC's in the vent stream.  Since these
parameters affect capital and annual costs, their values had
to be established.  Previous EPA studies show that at least
98 percent destruction efficiency can be met in a thermal
incinerator operated at a temperature of 1600°F and a
residence time of 0.75 seconds.16  Thermal oxidation of
                              5-9
-------
halogenated VOC requires higher temperatures.  Available data
indicate that a temperature of 2,000°F and a residence time of
one second are necessary to achieve at least 98 percent VOC
destruction efficiency for halogenated vent streams.17
     Auxiliary fuel will almost always be necessary for start-
up of the unit.  Also, in most cases, additional fuel must be
added to maintain the incinerator temperature.   With the
following assumptions, the amount of auxiliary fuel required
was estimated using the heat and energy balance around the
combustion chamber.18
     •    The reference temperature is taken as the inlet
          temperature of the auxiliary fuel (77°F). _
     •    No auxiliary combustion air is required (i.e., it is
          assumed that the oxygen content of the vent stream
          is at least 18 percent).
     •    Energy losses are assumed to be 10 percent of the
          total energy input to the incinerator above ambient
          conditions.
     •    At a constant moisture content, the heat capacities
          of the bleach plant vent streams entering and
          leaving the combustion chamber are approximately the
          same regardless of composition of the organics.
          This is -true for waste streams which are dilute
          mixtures of organics in air, the properties of the
          streams changing only slightly on combustion.
These assumptions and subsequent calculations of the fuel
requirements for a model vent stream are presented in a
separate document.19
     5.1.3.2  Development of Thermal Incinerator Capital
Costs.   The cost analysis for thermal incinerators presented
below follows the methodology outlined in the OCCM.  Equipment
cost correlations are based on data provided by various
vendors; each correlation is valid for incinerators in the 500
to 50,000 scfm range.20  Thus, the smallest incinerator size
used for determining equipment costs is 500 scfm; for flow
rates greater than 50,000, additional incinerators are costed.
                              5-10
-------
     Equipment costs are given as a function of total
volumetric flow through the incinerator and are accurate to
within 30 percent.  For halogenated streams, the equation used
in the costing analysis, after converting to 4th Quarter 1991
dollars, is as follows:2i
                    EC = 10,930 QTOT0'2355
where:
          EC   =    Equipment costs (4th Quarter 1991
                    dollars); and
        QTOT   =    Total volumetric flow rate through the
                    incinerator including any additional air
                    and fuel.
The cost for the conveyance of bleaching process vent streams
to the incinerator is not included in the incinerator
equipment cost.  The methodology for calculating costs for the
conveyance system for an incinerator is presented in
Section 5.1.2.
     Installation costs are estimated as a percentage of
purchased equipment costs and include auxiliary equipment,
instrumentation, sales taxes, and freight.  Direct and
indirect installation costs for thermal incinerators have been
incorporated into the total capital investment.  The total
capital investment is estimated at 1.61 times the purchased
equipment cost.
     5.1.3.3  Development of Thermal Incinerator Total Annual
Cost.  Annual costs for the incinerator system include direct
operating and maintenance costs,  as well as annualized capital
charges.  The bases for determining thermal incinerator annual
costs are presented below.
     The utilities considered in the annual cost estimates
include natural gas (auxiliary fuel) and electricity
(incinerator fan) .  The fuel and electricity costs w'ere
assumed to equal $3.48 per 1,000 cubic feet of natural gas and
$0.04/kW-hr, respectively.   The procedure for estimating the
                             5-11
-------
electricity requirement is described in Chapter 3.0 of the
OCCM.13  The procedure for estimating the natural gas
requirement was presented in Section 5.1.3.1.
     For this cost analysis it was assumed that the
incinerator requires 0.5 hour of operating labor per 8-hour
shift.  Maintenance labor requirements are assumed to be
identical to operating labor requirements.  Supervisory cost
is estimated to be 15 percent of the operating labor cost.22
Maintenance material costs are assumed to be equal to
maintenance labor costs.
     The annualized capital charges include capital recovery
charges as well as taxes, insurance, administrative and
overhead charges.  The capital recovery cost was calculated as
described in previous sections.  Taxes, insurance,  and
administrative costs were assumed to be 4 percent of the total
capital investment.  Overhead was estimated to be 60 percent
of the total labor and maintenance costs.23
5.1.4  Scrubber System Costs
     Scrubber costs were developed for two scenarios.
Scrubber systems were applied as secondary control to remove
acid gases from the incinerator exhaust after combustion of
halogenated bleach plant streams (i.e., post-incineration
scrubbers).  Scrubbers were also used as a primary control for
bleach plant vent streams, without incineration (i.e., stand-
alone scrubbers).  (However, based on recent industry
comments, stand-alone scrubbers could be acting as emission
points for methanol.  Scrubber effluent could also emit
volatile HAP's.)  Design considerations for the two scrubbing
scenarios described above are presented in the following two
sections.
     5.1.4.1  Post-Incineration Scrubber Design Considerations
Affecting Costs.  Scrubber systems consist of the following
major equipment:  quench chamber, packed tower, pump,
ductwork, and fan.  Post-incineration scrubber systems are
designed to remove acid gases formed during combustion of
halogenated organics.  System elements and design assumptions
                             5-12
-------
specific to this analysis are based on a waste gas stream
(i.e., incinerator exhaust) with hydrochloric acid (HCl) as
the most prevalent pollutant.
     General scrubber design specifications are presented
in Table 5-4.  Column diameter and height are the primary
design parameters that affect the capital cost of the
scrubber.  These design parameters establish the column shell
geometry and the amount of packing required.  The design
procedure assumes no heat effects are associated with the
absorption process and that both the gas and liquid streams
are dilute.  The liquid-to-vapor flow ratio is calculated from
the inlet and outlet gas and liquid stream flow rates and is
assumed to be constant through the scrubber.
     The column diameter was estimated based on mass transfer
equations in the literature,24,25,26,27,28,29,30
using characteristics of the model vent stream, the absorption
liquid (caustic solution), the packing material,31 and an
assumed column flooding condition of 60 percent.  For this
analysis, the diameters ranged from 3 to 15 feet, depending on
the flow rate of the model vent streams.  A detailed
discussion of design procedures is presented in Chapter 9 of
the OCCM.32
     The height of" the packed column was calculated by
determining the number of theoretical transfer units required
to obtain the desired removal efficiency and multiplying by
the height of a transfer unit.  The number of overall transfer
units was estimated using the equilibrium-operating line
graph, based on inlet and outlet conditions.  For this
analysis, the column height was approximately 30 feet.
     5.1.4.2  Stand-Alone Scrubber Design Considerations
Affecting Costs.  The stand-alone scrubber system consists of
the same major equipment as the post-incinerator scrubber
system.  The design assumptions were based on reported
industry chlorine and chlorine dioxide gas scrubbers.33
Information on one scrubber indicated that 99 percent chlorine
reduction was being achieved using a five percent caustic
                             5-13
-------
TABLE  5-4.
DESIGN PARAMETERS FOR POST INCINERATION SCRUBBER
                   SYSTEM
          Parameters
                              Values
Waste gas flow rate entering
absorber

Temperature of waste gas
stream (prior to quench
chamber)

Pollutant in waste gas

Concentration of the Hcl
entering absorber in waste
gas

HC1 removal efficiency

Scrubbing liquid
Packing type
                   400 to 80,000 scfma


                   2,000 °Fa-



                   HC1

                   100 to 15,000 ppmv



                   99 percent  (molar basis)

                   Caustic solution (white
                   liquor, E-stage filtrate),
                   5 gal/1000  ft3

                   2-inch ceramic saddl-es or
                   Raschig rings	
  The incinerator off-gas passes through a quench chamber
  which reduces the waste gas flow rate and temperature prior
  to entering the duct to the scrubber.
                             5-14
-------
solution (sodium hydroxide).  Most scrubbing solutions were
from existing caustic sources, such as white liquor, E-stage
filtrate, and weak wash, and based on available information,
scrubbers using these media can also achieve a 99 percent
reduction in chlorine.  An existing source of caustic solution
was assumed for this costing analysis.  For the cost analysis,
the liquid to gas ratio and column height were given based on
analysis of actual scrubber data and the diameter was varied
based on a vent stream flow of 53 Ib-mole per hour cubic foot
through the column.
     General scrubber design specifications are summarized in
Table 5-5.  The detailed design procedure used to select the
stand-alone scrubber variables is described in a separate
memorandum.19  Costs were estimated for a scrubber system from
cost factors provided in Chapter 9 of the OCCM.34  The
diameter for the scrubber ranged from 4 to 18 feet for systems
scrubbing vent streams from 2,000 to 80,000 scfm.  The
representative column height was assumed to be 27 feet with
15 feet of packing.19  A liquid to gas (L/G) ratio of
50 gallons per 1,000 ft3 was assumed.19
     5.1.4.3  Development of Scrubber Capital Costs.-  The cost
methodology for the scrubber (both post-incineration and
stand-alone) follows the procedure outlined in Chapter 9.0 of
the OCCM.34  The main components in scrubber cost are:  tower,
packing, and ductwork to the scrubber.  The following equation
was used in the cost analysis for the tower, after conversion
to 4th Quarter 1991 dollars:
                  EC =  (115,$/ft2) *  (S,ft2)
where:
          EC   -    Equipment cost (4th Qtr 1991 dollars);
          S    =    Column surface area (ft2),  approximated by
                    TT * D (HT + D/2) ;
          D    =    Diameter of the tower (ft); and
          HT   =    Height of the tower (ft).
     The cost for the column packing was based on the packing
volume.   The cost for 2-inch ceramic saddles or raschig rings
                             5-15
-------
 TABLE 5-5.   DESIGN PARAMETERS  FOR STAND-ALONE  SCRUBBER SYSTEM
          Parameters
            Values
 Waste gas flow rate entering
 absorber
 Temperature of waste gas
 stream
 Pollutants in waste gas
 Chlorine removal efficiency3
 Scrubbing liquid

 Packing type

 Packing height
 Column height
2,000 to 80,000 scfm
140 °F
C12/ C102, HC1, Methanpl,
Chloroform
99 percent (molar basis)
Caustic solution (white
liquor, E-stage filtrate), 50
gal/1,000 ft3
2-inch ceramic saddles or
Raschig rings
15 feet
27 feet
a  Removal efficiencies for other compounds range from 0 to 99
   percent and are documented in a separate memorandum.35
                             5-16
-------
is identical at $20 per cubic foot.34  The methodology for
calculating costs for the conveyance system for a scrubber
system is the same as for the conveyance system to a
combustion device presented in Section 5.1.2.
     The total capital investment was estimated to be
2.20 times purchased equipment costs and include auxiliary
equipment, instrumentation, sales taxes, and freight.34
     5.1.4.3  Development of Scrubber Annual Cost.   Annual
costs for the scrubber system include direct operating costs,
such as labor costs, utility costs, maintenance costs,
operating material costs, and wastewater disposal costs and
indirect operating costs, such as total annualized capital
charges.
     The cost for operating materials include that of the
absorbing liquid used in the scrubber.  According to a survey
by the EPA's Office of Water, many mills in the pulp and paper
industry currently purchase caustic (sodium hydroxide [NaOH])
for other mill purposes.11  In many cases, caustic solutions
from other mill processes (i.e., weak wash from the chemical
recovery loop) are used in the scrubber by supplementing with
fresh caustic as necessary.  The caustic used in the scrubber
may then be used in the bleach plant extraction stage or it
may be disposed of for a negligible cost with the remainder of
the mill wastewater that does not require control for air
emissions.36/37  For this analysis, water and caustic
costs were assumed to be negligible because the scrubbing
medium was assumed to exist on-site.19
     The utility considered in the annual cost estimates is
the cost of electricity.  Electricity cost is dependant on the
energy required to operate the fan and the pump to overcome
the pressure drop in the column.  For this analysis, an
electricity cost of $0.04/kW-hr was used.11
     The scrubber system maintenance and operating labor
costs,  supervisory costs, capital recovery charges as well as
taxes,  insurance, administrative and overhead charges were
                             5-17
-------
calculated as described in Section 5.1.3, with the only
exception being that a 15 year equipment life was assumed.
5.1.5  Steam Stripping Costs
     This section discusses steam stripper design
considerations affecting cost and the general methodology used
to develop capital and annual costs for steam strippers.  The
costing methodology and assumptions documented in this section
are those used in the proposed rulemaking package.  Though
industry has commented on the basis and additional information
is being developed, the results have not been revised to
reflect any changes at this time.  Specific areas for future
consideration are identified in the text of this section.
     A survey was conducted by the American Paper
Institute/National Council of the Paper Industry for Air and
Stream Improvement (API/NCASI), and of the 140 responses, 31
mills reported the use of strippers to control emissions from
wastewater.  Based on these data, approximately 67 percent of
these mills integrate the steam stripper into the evaporator
set and 33 percent use stand-alone steam strippers.38
Therefore, the (industry-wide) average costs presented in this
analysis are prorated for these percentages.  (Industry has
recently commented that the questionnaire was misinterpreted
and that a lower percentage of mills use integrated steam
strippers.)  For facilities that are not planning joint
evaporator upgrades, it would be less expensive not to
integrate and to retrofit the steam stripper into the
evaporator system.  The following discussion presents the
design and cost methodologies for both integrated and stand-
alone steam strippers.
     5.1.5.1  Steam Stripper Design Considerations Affecting
Cost.  Factors affecting the costs for steam stripping include
the steam usage (annual costs), tower height and diameter
(capital and annual costs), and the stripper configuration
(tray vs. packed-bed) (capital and annual costs).  The most
sensitive parameter for costing is steam use; therefore, any
adjustments to the proportion of mills using integrated versus
                              5-18
-------
stand-alone systems would have the most effect on costs for
controlling air emission from wastewater.  The steam stripper
system design basis included a steam-to-feed ratio of 0.18 kg
steam per liter of wastewater (1.5 Ib/gal) which achieves a
90 percent removal efficiency for methanol based on
representative data of pulp mill steam stripper
performance.39  The stripper was assumed to be a sieve tray
column with 8 theoretical stripping trays.38
     The column diameter and the size of the auxiliary
equipment are a function of the wastewater feed rate.  The
column must be wide enough to provide a desired (low) pressure
drop and liquid retention time in the column using
correlations developed to prevent column flooding.
     An integrated system uses steam from the evaporator set
for operation.  Due to the use of steam from the evaporator,
the use of fresh steam for an integrated system is much lower
than that of a stand-alone system.  The steam does lose some
of its heating value due to use in the steam stripper
(approximately 6 to 12 percent of typical boiler
capacity).40  Consequently, it must be supplemented with
make-up steam from remaining boiler supply for use in later
effects.  While it is not expected that an additional boiler
would be required in this case,  dedicated use of this steam
could limit future operational flexibility.
     It was assumed that the overhead stream from either
(integrated or stand-alone) system would be ducted to an
existing combustion device and would contribute some heat
value; however, this heat value will be partially offset by
the increased heat requirement to heat the high moisture
content in the vent stream.  In practice, a fuel-rich overhead
stream is obtained by including reflux in the stripper design.
Such a design would incur costs for the reflux tank and
associated condenser, yet produce a recovery credit for using
the overhead gases as fuel.38
     The cost algorithm used in evaluating national impacts
accounted for a recovery credit of $73,400 per year,  based on

                             5-19
-------
the approximated fuel value of the organics in the overhead
stream; however, that costing approach did not include feed
tank costs or reflux tank and condenser costs for the stand-
alone system, nor did it assume that any equipment other than
the sieve trays and pumps was constructed of stainless steel.
The costs for the cooling load on the reflux condenser were
also not included.  In practice, the recovery credit is
greater than the credit used in the analysis, but the system
capital and annual costs including the items listed above are
greater.  The resulting annual costs are within 15 to 20
percent of those presented in this document.
     5.1.5.2  Development of Steam Stripper Capital Costs.
The capital costs for the steam stripper system are based on
the following equipment components:
     •    Reflux tank (for integrated system);41
     •    Steam stripper column (including column shell,
          skirts, nozzles, manholes, platforms and ladders,
          and stainless steel sieve trays);42/43
     •    Flame arrestor;44
     •    Pumps;45 and
     •    Feed Preheater.46
All costs are for carbon steel construction except for sieve
trays and pumps.  It was assumed that these components would
be constructed of stainless steel because they are subject to
the greatest wear and are exposed to the harshest conditions.
No capital costs for additional boilers or cooling towers were
included.
     The total capital investment for a steam stripper system
is calculated to be 2.20 times the purchased equipment costs.
The purchased equipment cost includes costs for the -equipment
components, auxiliary piping (additional piping for combining
wastewater streams and vent lines), instrumentation, sales
tax, and freight.
     Stainless steel construction cost factors are included
for comparison because facilities with corrosive wastewater
streams  (i.e., high pH) will require a steam stripper system
                             5-20
-------
constructed of a corrosion-resistant material.  Equipment
costs for stainless steel were estimated from the carbon steel
costs, using a factor for conversion from carbon steel cost to
304 stainless steel cost.  Table 5-6 presents the stainless
steel cost factor for each equipment component.
     5.1.5.3  Development of Steam Stripper Annual Costs.  The
total annual cost is the total of all costs incurred to
operate the steam stripper system throughout the year.  The
annual operating costs comprise direct and indirect charges.
Direct annual costs comprise expenses incurred during normal
operation of the steam stripper process, including utilities,
labor, and maintenance activities.  For this preliminary
analysis, it was assumed that existing steam capacity and
cooling water would be used.
     Electricity is needed to operate pumps and other
electrical components in the system.  The electricity required
for the pumps is calculated using design flow rates for each
pump and assuming a developed head of approximately 37 meters
(120 ft)  of water and a pump efficiency of 64 percent.  For
this analysis, electricity cost is assumed to be
$0.04/kW-hr.1]-  The steam costs are estimated using the design
steam loading of 0.180 kg of steam per liter  (1.50 Ib/gal) of
wastewater feed.  For integrated systems, make-up steam use is
approximately 12 percent of the steam use for the stand-alone
system.40  For this analysis, the steam cost is assumed to be
$4.02/Mg.1:L
     The steam stripper operating and maintenance labor costs,
maintenance material costs, supervisory labor costs,
administrative and overhead charges, capital recovery charges,
taxes, and insurance were calculated as described in
Section 5.1.3, with the only exception being that at 15 year
equipment life was assumed.
5.2  CONTROL OPTIONS COSTS
     Table 5-7 presents a summary of total capital investment
and total annual cost for controlling an example mill using
the control options presented in Chapter 4.0.  The example
                             5-21
-------
           TABLE 5-6.  STAINLESS STEEL COST FACTORS
   Equipment component      Stainless steel cost    Reference
	factor	

 Steam stripper  column -              1.7                 42
 shell

 Reflux tank                         2.4                 45

 Feed  preheater            0.8193  +  0.15984  *  (In A)      46
                             where A is  in ft2
                             5-22
-------
W
    (0
               0)
                      (0
                      (0
 O  nj  O
 0)  0) 4->
Q S  W
                                   o
                                   o
                                   o
                                  CO
                                  (N
                                  o
                                  o
                                  o

                                  o
                                  vo
                                  00
                                 g
                                 a
                                 a
                                 o
                                 in
                                 g
                                <4-l
                                 O
o
o
                                H
                                in
  03
  rH W
  0) rH
 X! 0) rH
  w :$  nj
  (0 O  0)
  5 4J  W

 4-> 4-> 4J
 C C C
 <0 nJ ro
 •H rH rH
 a a a

 x: x: x:
 u o  o w
 (0 (0  rC ,*
 0) 0)  0) C
rH rH rH flj
CQ CQ CQ 4J
03
0)
rH
3 -

MH
O
C
Combustic

**
03
4J
C
0)
03
O
rH
0
c
0)
pulping v
capture (
o
.4->

>i
essar
o
0)
c
0)
rH
0)
x:
yance
and conve
g
an existi
0)
u
•H
>
0)
T3
i
C
combustio


iw
o

w
4-»
C
0)
>

w
4J
C
0)
>
Scrubbing
bleaching
(combined
                   o
                   o
                   o
                    V
                   o
                   •**
                   00
                  o
                  o
                   **
                  o
                  (N
                 a
                 a

                 o
                 in
                 H
                                   E
                                  M-l
                                   O
                                   (0

                                  o
                                  o
                                                Q)
                                               X!
                                                W
                                                       (0
                                                       a)
                                                       W
                                                         w
               •p -p  -p
               c  c  c
               (0  (0  flj
               •H rH  rH
               a a a


               o o  "6
               (0 (0  «J
               0) 01  0) C
              rH rH rH flj
              CQ CQ CQ .p
                                                        T3
                                                         Q>
              j^
              o  &>     o>
            •H  c TJ  c
            4-> -H 0) -H
              W X! IS XJ .
             300
            Xl  «J H
            g  0) rH
            O
                                                        o
                                                        o
                                                        o
                                                          *k
                                                        o
                                                        o
                                                        a\
                                                        o
                                                        o
                                                        o
                                                         •«.
                                                        o
                                                        o
                                                        in
                                                         *.
                                                        n
                                                       o
                                                       in 5
                                                       n g
                                                        - a
                                                       H a
                                    o g
                                    o ^
                                    tn rH
                                     * (0
                                                     a     g
                                                     O    H 0)
                                                     ,   -P O 4J
                                                     >H nj 4J to
                                                     "   " «J W
                                                           >H C
                                                               0)
 4->  C
 W  Q)  O
 tt) 'O  aT3
 D^ C  (0 C
•H O  > O
Q O U O
                                                                     o>  w
                                                                    •p  g
                                                                     (0  to
                                                                     £  0»
                                                   C
                                                   o
                                                  •H
                                               C 4J
                                               n)  ui
                                                                 a4->  4->     4J  g
                                                                 a  w  w  >,     o
                                                                •H  nj     XI  0)  O
                                                                 >H  S  -O     O
                                                                4->     0)
                                                                 w
                                                       x)  w
                                                       3 .JJ
                                                      r.  5 S  5 C
                                                      C -H •*  S-._j
                                                   g-H J3
                                            U  X) 
                                                       O  0)    4J  3 O
                                             -   .  .     0)
                                             O  0) 4J  O
                                             H  > W-H
                                             H  C-H  >
                                             00X0)
                                             4H  O  0) T>
                                                                            O
                                                                            in  g
                                                                            iH  <4H
                                                                                O
                                                                            <*H  W
                                                                            o
                                                                                o
                                                                            c  o
                                                                            O  O\
                                                                           •H   ^
                                                                           4-> in
                                                                            nj
                                                                            rH  U
                                                                           4-1  (0
                                                                            C  3
                                                                            0)
                                                                            O  0)
                                                                            C 4->
                                                                            O «J
                                                                           O >H

                                                                           (0 O
                                                                              rH
                                                                           X! 
                                                                           •H Q)
                                                                           s x:
                                                                           o  w
                                                                           (/]  0)
                                                                              o
                                                                          o  ^
                                                                          O  3
                                                                          O  O
                                                                           *  w
                                                                          o>
                                                                          CM 13
                                                                              0)
                                                                          W   01
                                                                          (0   O
                                                                          >  rH
                                                                              o
                                                                          w   c
                                                                          0)   0)
                                      3
                                      en
                                      o
                                    • rH
                                  (0  O
                                  0)  C
                                  rH  0)
                                  3
                                  03  &i
                                  O C
                                                                                                           rH
                                                                                                           o
                                                                           C
                                                                           (0
                                                                                                   O
                                                                                                   C'..
                                                                                                   0)  3
 0) 0)
 r-l
•H
 3
                                                                                                      W
                                                                                     0)  O
                                                                                     rH  rH

                                                                                    4.B
                                                                                     (0  0]
                                                                                    x:
                                                                                    •P  rH
                                                                                        o
 C  £
 o  g
•H  a
-P  a
 «j
    o
•H O
 nj o
4J  -.
0] rH
C
                                                                            0)
                                                                            >H  C
                                                                            3  O
                                                                            03 -H
                                                                            0 4->
                                                                   4J
                                                                    C 0)
                                                                   •H 4J
                                                                    O n]
                                                                    a rH

                                                                    c >
                                                                   o o
                                                                   •H rH
                                                                   V)  «M
                                                                                           O  >H
                                                                                           C 4->
                                                                                           0)  C
                                                                                               0)
                                                                                           JH  O
                                                                                           0)  c
                                                                                          4->  O
                                                                                          <4H  O
                                                                                  •H  0)  g 4->
                                                                                   g x:  a-H
                                                                                  w EH  as
                                                                                                a xi
                                                         5-23
-------
mill is identical to the model chosen for the examples given
in Chapter 4.0 (i.e., pulping capacity 1,000 tons per day,
pulping model Pi and bleaching model Bl, as given in
Appendix C).   This model was chosen since it is used most
often in representing mills in the industry.  The assumption
was made that this mill has existing baseline controls, as
discussed in the examples in Chapter 4.0.  Vents assumed to be
controlled at baseline include the digester relief vent,
digester blow gas vent, and the evaporator noncondensible gas
vent.  The costs to control these vents is not included in the
cost examples to follow.  Industry has commented that the
control of evaporator condensate streams is less than what has
been assumed for this analysis.  However, for the purpose of
this analysis, it was assumed that all pulping wastewaters
generated are steam stripped due to the high concentrations of
methanol present in the model (PI) condensate streams.  This
analysis also assumed that bleach plant wastewaters, including
scrubber effluent, were not steam stripped.
     A detailed breakdown of the costs for the selected
control options (as in Chapter 4.0) are presented in
Tables 5-8 to 5-12 for the example 1000 ton per day (TPD)
facility.  Brief discussions are given below.
 1    The example costs for controlling pulping vents are based
on ducting the vents to an existing combustion device.  The
costs to convey the vents are based on two procedures.  Points
that do not require enclosures are combined into a main duct
which is piped to a retrofitted existing combustion device.
The costs for controlling these vents are presented in
Table 5-8. The pulping points that require enclosures  (i.e.,
rotary vacuum pulp washer, knotter, and decker/screen) are
enclosed and then combined in a second main duct and piped to
the appropriately retrofitted control device.  The costs for
controlling these vents are presented in Table 5-9.
     Two potential scenarios to control bleaching process
vents (as discussed in Chapter 4.0) were selected for examples
                              5-24
-------









w
w
s
o
s&
o y
^>
^ w
" Q
H
§§
W p^
EH
W
O^w
S
S! g
g8
2 rj
2
^* i i
g_i
2 uj
H H
fX £j
tJ
S s
^
rJ rH
*~^ S
SK
w
o
s
^
o
fa
w
CO
8

CO
1
in
TABLE






^
tn
O
o _^
^^«
^^ «^ _^
fO
4»)
o
EH

•P
(0
o
O
.p _
s^
c
o
Cu
§
u





.p
U)
o
o

V>4
o

N O
•H 4J
w o
tO
c
0)

p.
•H
D1
U






•P
C
Q)
C

o
o
-p
o
u


















o o o
o o o
o o o
O H rH*
in
















to X! ^
0} 4J 0) ^
•P &> -P Q)
Q) C 0) -P
g 0) g (1)
(0 iH (0 g g
-H W -H  -p
C (0
•H 0
0
rH
(0 rH
•P (0
•H 3
a. c
m c
O (0

i— 1 *-s. rH
«J H n)
•P U 4J
0 EH 0
EH — EH






ft!

X!
•P
•H

C
-p
H
rH 3
O O
C rH
LJ (li
(0

!







CO*
CO
o
.p
c
0)
1
• H
3
D1
0)
T3
0)
Ul
(0
X!
o

3
a
CO
(0

c
0)
•H

u1
0)
ITS

CO
-p
(0
o
o
4J
C
(U
g
•H
3
O1
0)
+J
X!
-P
Tf
0)
s assu
10
3

-P
H
A
5-25
-------

^-.
w
w
u
a
o
w
w

H
EH
H
£
D

W
i
w
9 w
H f,
0 H
55 ^
fa ^
§
o
S 2
H n
«2
REQUI
MBUST:
gs
w 2
>~> 2
^ H
U ^
s2
H
S *

S
J
U
Q
0


OS
O
fa

CO
EH
C/l
O
U
.
Cfi
in

H
CQ
rt!
EH

-P
U

O ^_ %
CO s~>'
-P
O



, )
+^
(0
o
4J ^
m 
o
a
0
u




-p
01
o
o
0) r4
N O
•H .p
01 U
cd
•P IM
c
 tj *2
CO O
Q) 5 X
B 4J 0
a u c o
•H 3 CO C
3 Q fa X
CF
H
























Ul
<3)
X
O
•rH
x:
.p
•
c
•H
in
o
O





































O
O
o
H
rH
H








rl
0)
•P
(U
CO
•H
T3
•
C
•H
in
,











j_i
o
CO
(U

CO
(1)
E
CO
rH















O
O
o
en
•»











ca
0
U]
•H
TJ
o
rH














O
(Q
•H
T3
Q)
3
•P
a
3
a















o
o
o
^r
H







-P
Ul
O
O
4J
(U
g
a
•H
3

0)
4H
O
3
W




Ij 1 LA
U C
o a)
u e

•P U)
C (I)
Q) >
E C
CU -H
•H
3 rH
D1 CO
Q) 4J
•H
"O D<
0) CO
U) O
CO
r* 	 «_j 	
«JM ^^ r^ ^^
O U (0 H
r< W 4J U
3 0< O EH
CU ^- EH •—


0 j O
0 0
0 0
in 10
vo - n
rH -





O O O O
o o bo
O O 0 O
o in co co
in co co in
CM CO CM
~






0) (U
tj If
3 3
in H
co
01
-P
01
0
0
•p
o

Q>
•H
3
cr
0)

.p
CO
X!


T5
0)
3
01
01
CO
01
• a
S Z

C
•H

rH
CO
.p
•H
a,
CO
o
rH
CO
•P
O
EH

0



T3
C
cO
)H
0)
•p
4J
O
C


CD
4J
^
O
^i
fll
3
W
0
H
O
c
Q)
0)
rH
CP
C
•H
O
TJ
CO

o"
o
O
O
n
CM •
•^ Jg
0
01 cO
-P o
^
O 0
ao
ftO
3 -
01 •*
VP
'O <«•
C —-
CO
01 a)
"O CD
O >-(
O 0
XI 01
r< IT
CD a)
JM t^
01 u
CO <0
5 T3


5-26
-------
                                     O
                                     o
                                     o
                                      *.
                                     r-
                                     CO
                                     CM
   ooo
   o   o   o
   ooo
o
n
n
            o
            a\
o
o
o
  *.
o
VO
CO
       w
      -p
       U]
       o
       o

      •P

      0)

      a
     •H
      3
      O1  U
      (U  W
      o
          CO
      g   H
      3    •
     W   H
             U
            O
            CN
              •

            CM
  U   H
  W   U

ja
*-«•
W
3
O
X)
i-H
W

<-8

(U
Q<
•H
04
>-^

4J
O
3
Q





U
H
v»>

4J
U
O
O

4J
C
0)
g
a
•H
3
cr
H


4J
u
0
o
.p
c
(U
g
a
•H
3
tr
0)

73
0)
U
(0
.c
o
^
3
a«
-P
c
0)
g
4J
CO
(U
>

•H

«H
n)
.p
•H
Q<
(0
o

rH
(0
J->
o
EH


















H
O
EH


                                 O
                                 O
                                 O
                                 3
                                 C
                                (0
                                -P
                                O
                                EH
 W -O
 (U  0)
 cn-p
 «3  C
•P  0)
 ca  u
                                                   C 0)
                                                   n3 b
                                                      (0
                                             - o
                                           Q  5
                                              -P
                                              '0
                                           g
                                           O
                             (0  (fl
                            •P  a)
                             c  ^
                             0)  3
                             > T3
                                0)
                            ^  U
                            C  O
                                                 (0  (fl
                                                 0)  O
                                                 u  u

                                                T3 T)
                                                 C  C
                                           - 0)
                                          M  N
                                          0) -H
                                         JC  (0
                                          U]
                                          nJ .p
                                          5  C
                                             (U
                                          -  g
                                         ^  a
                                         (U-H
                                         5 3
                                         O D1
                                        •p (1)  .
                                               CO
                                        C T3 I
                                        o  a) in
                                           rH
                                        T3-H Q)
                                        QJ 03 rH
                                        W -P JQ
                                        
-------
Pi
o
EH

K
W
Z
H
U
z
H

o
H
CO
D
CO
53
W
CtJifl
EH «
CO W
CO
EH CQ

W Oj
> u
CO
Z **!
H
a x
U 00
W Q
r-3 W
CQ &
j J
j j
H 0
^p &4

J
W
Q
O
2
*«H
ft,


^
O
EH
O
U

e;
2

CO
EH
CO
o
u


H
H
1
in

w
i-3
CQ
rtj
EH

•P
CO
O
U ^
v>
r^ ^ ^ ^.
(^
•P
O
EH
4J
CO
O
o
4-> ^
m 
C ""
O
C^4
K
O
o




.p
CO
o
o
g
d) j_(
N O
•H JJ
CO O
ij _••

CO
H
•
H

CO
O -P
o c
a)
-p g
C -P
(U CO
g (U
a >
•H C
3 -rH
Q) rH
«3
T3 -P
0) -fH
co a
(0 (0
x: -* o
00
^ W rH -^
3 O* (CM
04 — 4J U
O EH














o
o
0
o
m
fM


















u
H
a,

*

H
VO
•
H








^
0
-p
(0

0)
c
•H
O
c
•H
H
U
EH















O
O
O
O
m
co
CNJ













r< J^
•P 0)
C 0)
0) g
rH (0
•H CO
. T3 3
•P O
.p 4_l • XI
O C rH
3 0-H 0)
•a o
O CO O
H H ** f>J


^
O
-P
(0
0)
c
•H
0
c
•H

o
-p
•p
0
3
T3
H
O
EH















O
0
0
in
in














^
X! -P
-P a)
en g
C ID
Q) -H
rH T3 CO
5
-P • O
<*H C XI
•rH rH
O (U
O CO
m •* vo





0)
O
XI
3

U
CO

o
.p
4J
O
3
T3
H
O
EH















0
o
o
*»
0
in














^i
a)
-P -P
(U X!
g en
(0 -H
•H 0)
•0 X!

. ,
•P 4J


in t^
H CM










•^
0)
XI
XI
3

O
CO
H
QJ
EH




O
O
O

o
(N
f)
^
«*



_









. O

4J 0
0 4->
T3 4J QJ
H 0 XI
O 3 XJ
EH -C 3
W tj
+ U 0
EH CO
O+ U
-P EH
(0 M
n o +
0) -P
C (0 ^
•H s-i a)
O Q) X!
C C XI
-H-rH 3
H O >H
U C JJ
EH -H CO



















H
U
EH
5-28
-------
«
g
i^C
K


H
U
S
H
§
£
H
W
D

W
s
« -.
EH-0
W 0)
*O
EH 3
*^ j-_l
^H r^
U O
> C
o
o o
a *-'
H
X OS
U W
< CQ
W CQ
iJ S
CQ OH
o
iJ CO
ij
H<
>H
iJ CQ
U
Q Q
O W
g &
b J
°0
J Ct,
0
&
EH
S
0
u

OS
o
PL,
W
EH
CO
8


•
H
H
1
in
W
i-3
CQ
<
EH

4J

O
O ^
_i 
i— I
(0
-p
o
EH

-P
CQ
O
O
J_l
+•* ^^^
§
W ^^
o
Qt
e
o
u




•p
IQ
O
O
V4
O
0) ^
N O
•H JJ
in u
«j
JJ <4-l
C
Q)
e
a
•H
3
O1
W







4J
Q)
C
O
U
§
o
O
-P
O
O

















O
0
o
^
o
n
CO
CN




















^^
U
<
£
•*-s
10
4-1
CQ M
0 0
O *J
nJ
r-l VJ
(0 Q)
3 C
C -H
C O
(0 C
•H
•H U
n)  n






O
-P
-P 0
O -P
3
T3 -P k
U O 0)
< 3 XJ
EH T3 X>
U 3
+ < ^
EH 0
b CQ
0 +
•P T3
n] k.C
^i O (0
0) ^>
c m ^
•H ^ Q)
O 0) XJ
C C XJ
•H -H 3
O 0 ^
<: c o
EH -H W



T)
^1 C
O (0
+j
(0 M
i-l 0)
0) XJ
C X)
•H 3
O fc
c o
•rH CQ

o o
4J -P XJ
^i
-P -P 0)
U U XJ
3 3 XJ
T3 T3 3
U O>-i
<  cu
o
^ 0
C M
n3 a
-P
4J
•H W
(0 O
(U U
CQ
•a
-a c
C (0
«J
Q) •
^ N O
CU -H i-l
£ CQ 1
CQ in
(0 4J
SCO)
a) H
- e xj
^ a «j
OJ-H EH
S 3
0 O1 C
•P CU-H
C T3 M
O Q) Q)
rH XJ
•O-H XJ
CU (0 3
CQ 4J ^
(0 CU O
CQ Q U

(0 XJ
5-29
-------





CO

i
EH
CO

w
EH
g
U
EH
CO
§

CD

H
CM
tD OJ
PL, PI]
CM
1-3 H
H p£
SC-|
1. '
W3

w s
o 3
o w
CO
fa
o <
»-5 O
o 55
OS H
EH CO
O
U

a
o
fa
EH
CO
O
U

.
CN
H
1
ID
W
03
EH




4->
CO
0
0 __
(0 ^"
-P
O
EH


4->
O

.p ^
5»% VJ°
r* >~'
O
ft
S
O
o




l_i
w
o
U

J^
o

4) ^
N O
•H ±>
CO 0
nj
C

IQ
U














o o o n o
O O O H O
O O O H O
• O O P** ^D
co in H o
VO H H









ft
43

o
l-l

M
0) CO
•p g
S_l QJ Q) O
Q) g g 4^
4-> 4J 3 (OP
^J I-H > c"0 *
t^4 *^n flj "^1 • ^J
O -P M-l (0
f*i jj 1 1 i[ [ it
f^ '[ j *j | ^ \^ frt jn
^ ^3 CM v^ u) C
CT> H CTi C* • Q) (
*<• l— 1 OJ rH rHOfaC


•o -->
0) >i
4J rH
fO C
JH O
cr>
-- O M
O Q) g C Q) -P
0) rH p M -H
C ft O X
0) 3 — » Q) W
g T3 >i rH >i g ft
ft Q) (0 










ft
A

O
H

*,
(0
g

4^
ft 4J
H
^3
x" §
3
J rH T3 JS
) ^>4 Q) O
JQ) QJ (0
) OH fa Q)





T3
0)
-P

&>
0)
C
C
£
w ~.
ft ^1
g rH
3 C
CM O












O
0
O
O
in
<7>








+
C
g

rH
O 0)
U g CO
(0 ft
nj <4H 3

^J >4"
+ * n
C +
w •^* r^
4J O
(!) 3 CO
X3 <-H Q)
Q) ^H M
>H (U >H
&l >H _»
CJ
H












O
O
O
o

(n







^^
+ o
C CO
g 0)
3 M
rH ^
O «J
O
(U
nj (0
>-l rH
4J ^-t
+ +
tj *> jn
0 C Pi
4J (0 g
(U ft
£ T3
Q) Q) C^
^i j Q)
04*^ +


10
4->
CO
O
o
T3 4-1
(U C
4-> (1)
1T3 g
& -H
4J D1
C 0)
•H
C TJ
O 0)
C U
^^ "" (0 ••
H P5?
pj ^ f^l
3 Cli











0 0
0 0
o o
0 O
o o
H H
rH H







CO
0)
rH
(C
U) C
o
+ -H
4J
(0 (C
C C
•H Q)
Cu G
"a S
4J
r*4 C
-H'H
rH +
••H
X X
3 (0
ri< 4J






^
0)
^ 4->
T3 «3
d) M
io oT
O> C
Q) -H
4J C
C 0
'i E

U U
(4 U
IX CU

5-30
-------







CO
W
PS
EH
CO

PS
%
5
EHTJ"
CO CO
SI
o o
2 C
H O
O-i U
g g
M
|4 04
iJ 04
H H
CH
iJ 05
W
Q S
o SJ
s w
EH
fa CO

id!
J
o e>
PS 2
EH H
2 W
0 D
U
PS
O
EH
W
O
CJ
CM
H
1
If)
pa
g





-P
W
o
o _^
rH<£
(Q
-P
O


-P
(0
O
o
.p ^
s 
C "~
o
B
o
CJ



4J
CO
0
o
M
O

CO M
N O
•H .p
W O
id
•P 
£3 CO
— p
T3 (0
CO M
-P en
M-P
CO --I
4-J ^
c o
CJ CJ -H C
U H H H -
« * ^^v_^ J
r^ o *c
CN CN VO CO H
. . . . CJ
rg M o o EH





-5"
(U
0) M
<0 0)
M -P
•P C O
C O 3
H H H
U U U
EH EH EH H
CJ
EH


O
0
O
o
o
H





O O O O O O
o o o o o o
o o o o o o
o o n o o o
in o t^ co o CN
OJ fl








+
+
^ (0
CO M
-P tn
id co
cn c
CO -H
•H C
tt g
«> r> CJ
. . <
O O EH




-P
— * -H
CJ T3
< CO ^*
EH M 73

W 10 ^-» -P
-P O O — >i T3 Id
10 O O TJ M CO M
O CO CO -P CT>
o B-sgP > id co
id TJ id id o M-P
ro -P -P -P CP CO C?-H^
3u)id nco M-P c u
CMP C O 3

id idco id-H nj>-'s_<—
rH CC CO CCJUO
-p  a
CO -H
i i ^
u -P
id (0
5 B
O CO
C M
•P . CO
id -P
c id
•H M
g CO -^
0 P >i
O C >H
•H CO
A C -H
-P • id -P
tn o
•P -P CO

c tn CD
3 C U -
O T3 CO n
a "o £ o*
O i M CO O
M O M rH
(0 Q* (0 fd
•H id i
•H 4J C
3 C O P
<4j rd O w

-------
in this cost section.  The first scenario is based on
combining and controlling the vents with a scrubber designed
to remove HC1 and chlorine (with some consequential volatile
HAP removal).  These costs are presented in Table 5-10.  The
second cost scenario is based on combining and controlling the
vents, first by incineration, then by ducting the incinerator
exhaust to a scrubber.   The costs associated with this
scenario are presented in Table 5-11.
  The example costs for wastewater streams are based on
combining the streams and controlling with a steam stripper,
with the overheads ducted to an existing combustion device.
The cost procedure is presented in Table 5-12.  The costs are
based on a weighted ratio of the cost of an integrated steam
stripper and a stand-alone steam stripper (0.67 and 0.33,
respectively), as discussed in Section 5.1.5.
  A comparison of costs for pulp mills of varying sizes is
presented in Table 5-13.  The mill sizes are small (500 TPD) ,
medium (1000 TPD), and large (1500 TPD).  The detailed cost
procedures for the medium mill are presented in Tables 5-8
through 5-12.  The same procedures were used to estimate costs
for the small and large mills.
                              5-32
-------












&••
x—'
p 1
CO
o
u
(rf
^*4
g
§

JJ
<
o
EH
CO
Q W
(5p U-J
^
^s cH
H
*~* CJ
H <
U CU
tg

EH O
2 2
'ESTME1
VARYI1
Z X
H EH '
»J ^>
rtj
EH CO
M ij
04 J
•< H
U g
rJ t-3
<1 W
EH Q
O O
EH g

fr, Ct
00
2 ^
o
CO
H
9
CU

O
u

.
n
H
1
in

3
HH
09
^3
EH








M
O
H


O
s
*"^


u
?J





o"
(X M

^
•tj °
s §
0. H
id
o

'H <

•rl
S




. .
O
o
o
in


O
£








4->
C
"o
cu
c
o
en
en
c
w










c
o
•H
^*
o



o
O
o
w
o
rH
"91

CO

o
o
o
o
rH
rH

CO-
o
o
o
o
oo
CM

CO-

o
o
o

ro
oo


CO-
O
o
O
*»
O
r-
rH
CO

o
o
o
oo
m


CO-



X
c
id
4J U
o
td CP
0 -1
c
X x id
Of 1 JJ
w HV
o m
4-1 rH 0)
o) XI en
c id
Bf£ r^
m o
i_i ni 1 1
M w +•
03 3 01



CO
0)

4-) 3
0 en
c o
rH
VM cn O
0 4J C
C 0)
C 01
0 > Cn
•rl C
4J O>-*4
cn c w
3 -1 -rl
.5 a 3
030)
o a. u
O '
o
O '
Vb
o
o
rH
CM
CO-

0
o
0
a
in
^

CO-
O
o
o
o
vO
•k
rH
CO-

O
o
o

o
in
n

CO
o
o
o
*,
$1,000

o
o
o
o
rH
CM

CO-





M
0)
£ 01
01 C
id 01
?m
w
.* u
Offl
UJ
0 . *-.
•4J M W
0) 01 14
C 4J 01
3 4J .*
0 O O
Lj f* rtl
W h4 UJ
CQ « Q



en
0)

3
en
O
rH
VM 01 O
O 4J C
C 01
C 0)
0 > Cn
•rl C
4j cn*ri
01 .C IH
3 "4 -I
jQ Oi 0-
S3 0)
a 14
0 '
o
0
w
o
o
«-•
rH
CO-

Ca
o
0
0
(*>
r»>

CO-
O
O
O
0
vO
00

CO-

o
o
0

O
cr>
CM

CO-
0
o
o
*,
0
o
CO-

o
o
o
0
vO
rH

CO-

0}
^
c
en id
j-4 en 4J
J3 01 rH
en 3 id
id O 0)
3 4J en

C C C
id id id
a* a a.
J3 JS JS
000
id id id
0) 01 01
CQ CQ CQ







at
en
-P
VM a>
O >

en en
c c
•H -4
XI O
3 id
14 0>
O rH
CO XI
0
o
o
*
0
o
o
(^
CO-

Q
O
o
o
o
m
r»
co-
0
o
o
o
o
n
»
CO

0
o
o

o
o
oo
«
m
co
o
o
o
*.
o
r-
vO
CM
CO-

O
o
0
o
n
vO
•
co-

co
^
c
en id
)-i en 4J
0) n
£ OJrH
en 3 id
id 0 0)
3 4J en

C C C

Oi P( pi
JS JS JS
000
id id id
01 01 0)
CQ CO CQ







CD
4J
VM C
0 0)

C XI id
0 Cn en
•rl C TJ C
JJ -rl 0) -r|
01 JS 3X1
3 O O XI
JS Id rH 3
6 COrH rl
O^H 0 0
U XI VM en
O '
o
o
*,
o
o
vO
^r
CO-

o
o
o
o
o
**!
CM
CO-
O
O
o
o
o
in
*
CO

0
o
o

o
o
o^
»
rH
CO-
o
o
0

o"
CM
vo
rH
V>

a
o
o
C3

00

CO-




^
C
a
3
3 0
rH ca a
XI 01 V4 0)
4J O 4J
M Id 4J Id
0) en id a
4J C M C
en 0) 0 0)
Q) -a a-a
Cn C id C
, j n *v O
"^ U ^ U
a o u o

* *


c
•MM *J 0
00) C "4
jj 01 jj
en id > m
C 3 3
••HO) , id o

Tj 3"° 8 o °
4J TJ C 4J Cn
co en o) id c
c 3 >i e -H oi
g -rl O 0) Id 4J O
Id Ol rH r* OJ CD -rl
01 -< rH C W -rl >
4J 3 0 O 4J X 0)
CO O
C
•r4
a

c
0
CO
01
'e
0)
4J -~-
C CO
01 4J
> C
01
0»
c
-^ IN
JS rH
O
id en
0) C
rH ~4
XI rH
«
0) 4J
£ 0
id
5-33
-------
5.3  REFERENCES
1.   Memorandum from Greene, D.B., Radian Corporation to Pulp
     and Paper NESHAP project file.  Brownstock Washer
     Enclosure Costs.  July 21, 1993.

2.   Memorandum from Greene, D.B., Radian Corporation to Pulp
     and Paper NESHAP project file.  Development of Gas
     Transport System Design and Costs.  September 27, 1993.

3.   Vatavuk, W.M., Estimating Costs of Air Pollution Control.
     Chelsa, MI, Lewis Publishers.  1990.  p.  74.

4.   Ref. 3, pp. 77, 78.

5.   Ref. 3, pp. 71-72.

6.   Memorandum from Greene, D.B., Radian Corporation, to Pulp
     and Paper project file.  Flame Arrestor Costs.
     August 2, 1993.

7.   Memorandum from Greene, D.B., Radian Corporation, to Pulp
     and Paper project file.  Rupture Disc Cost.  August 2,
     1993.

8.   OAQPS Control Cost Manual.  Fourth Edition.  U. S.
     Environmental Protection Agency, Office of Air Quality
     Planning and Standards.  Research Triangle Park, NC.
     Publication No. EPA 450/3-90-006.  January 1990.
     pp. 7-38 and 7-39.

9.   Ref. 8, p. 3-52.

10.  Municipal Waste Combustors - Background Information for
     Proposed Standards:  Cost Procedures, pp. 3.7-1 and
     3.7-2.

11.  Fax.  Rovansek, W., Radian Corporation - Herndon, VA, to
     Watkins, S.L., Radian Corporation - Research Triangle
     Park, NC.  July 16, 1992.  Operating costs from regional
     cost letters,  pp. 16 through 23.

12.  Ref. 8, pp. 2-26, 2-29, and 3-54.

13.  Ref. 8, Chapter 3.0.

14.  Memorandum from Seaman, J.C., Radian Corporation, to
     Project File.  Control of Pulping Vent streams in an
     Existing Combustion Device.  September 29, 1993.
                             5-34
-------
15.  Memorandum from Pandullo, R.F., Radian Corporation, to
     Barbour, W.J., Radian Corporation, Evans, L., U.S. EPA,
     et al.  Summary of April 11 Meeting to Discuss Thermal
     Incinerator Cost Issues.  April 27, 1990.

16.  Ref. 9, p. 3-8.

17.  Memorandum and attachments from Farmer, J.R.,
     U. S. Environmental Protection Agency, Emission Standards
     Division, to Ajax, B., et.al., August 22, 1980.  Thermal
     Incinerators and Flares.

18.  Ref. 8, pp. 3-31 through 3-34.

19.  Memorandum from Olsen, T.R., Radian Corporation, to
     Shedd, S.A., EPA/CPB.  Pulp and Paper NESHAP Selection of
     Bleach Plant Scrubber Design and Costs.  October 8, 1993.

20.  Ref. 8, pp. 3-42 through 3-44.

21.  Ref. 8, p. 3-47.

22.  Ref. 8, p. 2-25.

23.  Ref. 8, p. 2-29.

24.  Perry, R.H., D.W. Green, and J.O. Maloney.  Perry's
     Chemical Engineers' Handbook.  Sixth Edition.  New York,
     McGraw-Hill Book Company.  1984.  p. 3-78.

25.  Ref. 24, p. 3-249.

26.  Ref. 24, pp. 3-75 and 3-76.

27.  Ref. 24, p. 14-16.

28.  Geankopolis, C.J., Transport Process and Unit Operations.
     Second Edition, Boston, MA.  Allyn and Bacon, Inc.  .1983.
     p. 798.

29.  Felder, R.M., and R.W. Rousseau, Elementary Principles of
     Chemical Processes.  Second Edition, New York, NY.  John
     Wiley & Sons.  1986.  pp. 622 through 624.

30.  Ref. 8, p. 9-65.

31.  Buonicore, A.J., and L. Theodore.  Industrial Control
     Equipment for Gaseous Pollutants.  Volume I.  Cleveland,
     OH, CRC Press, Inc., 1975.  pp. 74, 105, and 106.

32.  Ref. 8, pp. 9-14 through 9-35.
                             5-35
-------
33.  Bleach Plant Chlorine and Chlorine Dioxide Emissions and
     Their Control.  Technical Bulletin No.  616.  New York,
     National Council for the Paper Association for Air and
     Stream Improvement,  Inc.  September 1991.

34.  Ref. 8, pp. 9-36 through 9-46.

35.  Memorandum from Olsen, T.R., Radian Corporation, to
     Shedd, S.A., EPA/CPB.  Model Scrubber Removal
     Efficiencies.  September 17, 1993.

36.  Telecons. Brown, H.P., to various mills.  Scrubbing
     medium.

37.  Telecons.  Brown, H.P., Radian Corporation - Research
     Triangle Park, NC,  with Rovansek, W.,  Radian Corporation
     - Herndon, VA.  Wastewater Treatment Costs.
     January 13, 1993.

38.  Memorandum from Fortier, G.E., Radian Corporation, to
     Pulp and Paper NESHAP Project File.  Basis for Pulp Mill
     Steam Stripper Costing.  September 30,  1993.

39.  Memorandum from Fortier, G.E., Radian Corporation, to
     Pulp and Paper NESHAP Project File.  Design Steam-to-Feed
     Ratio of a Steam Stripper in Pulp Mills and Development
     of Fraction Removed Values.  September 3, 1993.

40.  Burgess, T.L., Chemetics International, Inc.  The Basics
     of Foul Condensate Stripping.  Environmental Issues-1990.
     A TAPPI Press Anthology.   pp. 348 through 352.

41.  Damle, A.S., and T.N. Rogers, Research Triangle
     Institute.  Air Stripper Design Manual.  Prepared for
     U. S. Environmental Protection Agency,  Office of Air
     Quality Planning and Standards, Research Triangle Park,
     NC.  May 1990.  pp.  17-18.

42.  Estimation Costs of Distillation and Absorption Towers
     via Correlations.  Chem. Eng.  Vol. 88, No. 26.
     December 28, 1981.   pp. 77-82.

43.  Peters, M.S., and K.D. Timmerhaus.  Plant Design and
     Economics for Chemical Engineers.  Third Edition.  New
     York, McGraw-Hill Book Company.  1980.   pp. 768-773.

44.  Telecon.  Gitelman,  A., Research Triangle Institute, with
     Oakes, D.  Flame Arrestor Costs.  September 1986.

45.  Estimating Process Equipment Costs.  Chem. Eng. Vol. 95.
     No. 17.  November 21, 1988.  pp. 66 through 75.
                             5-36
-------
46.  Estimating Costs of Heat Exchangers and Storage Tanks Via
     Correlations.  chemical Engineering Volume 89, No. 2.
     January 25, 1982.  pp. 125 and 127.
                             5-37
-------
     6.0   DATABASE SYSTEM FOR ESTIMATING NATIONAL IMPACTS

     This chapter describes the development and use of a
database system for estimating the national impacts of
regulatory alternatives on the pulp and paper industry.  The
database system was designed to provide estimates of national
uncontrolled air emissions, national baseline air emissions,
and national impacts of air control options (HAP emissions
reductions, costs, and secondary impacts).  In addition, to
allow joint evaluation of the overall impact of air control
options and water effluent guideline control options, the
database system generates summary tables of impacts using the
calculated air control impacts and water control impacts that
were provided by the EPA Office of Water.
     Figure 6-1 presents a flow diagram of the process for
estimating national impacts.  The remainder of this chapter
discusses the data inputs, the steps for calculating air
emissions, air emission reductions, control costs, electricity
and fuel use, and the generation of summary output tables for
these joint air and water control impacts.
6.1  DATA INPUTS
     As described in previous chapters, extensive data
gathering efforts and review were conducted to characterize
the pulp and paper industry with regard to processes and their
emissions and current levels of control on a mill-specific
basis.  A database containing information (e.g., capacity,
wood type) on each pulping and bleaching line for all mills
considered for regulation by the EPA was developed to estimate
national impacts of control options.1/2/3 (This mill-specific
database contains confidential business information and is,
therefore, not publicly available.)
                              6-1
-------
                       Data Gathering & Review
                   (Processes, Emissions, & Controls)
                      Model Pulping & Bleaching
                            Process Units
                     Model Process ,
                         Units     i
Emission
 Factors

ig
Dn
•s



Pulp & Paper
Mill Database
(Mill Specific)
                                                    Industry
                                                Characterization
                                                  (Model Mills)
             Assign
            Baseline
            Controls
                                             Calculate Uncpntrolled
                                                 Air Emissions
                                               Calculate Baseline
                                                 Air Emissions
  Identify
Air Control
  Options
                                           Water '
                                          Control
                                          Options
                                                  Calculate Air
                                                     Control
                                                     Impacts
     8 Involves reassignment of model
      process units if water control
      options require process
      modification

     b Provided by EPA Office of Water
                                            Water
                                           Control
                                           Impacts
                   Emissions & Control Impacts
                                                           Environmental
                                                       Air
                           Water
                                                                                Costs
                   Figure 6-1.  National Impacts Estimation Process
                                            6-2
-------
     Because emissions data were not available for each mill
included in the pulp and paper mill database, a model process
unit approach was taken to estimate national emissions.
Chapter 4.0 summarizes the 30 model pulping and bleaching
process units that were developed to represent the industry.
These models included, for each emission point, a design
capacity-weighted emission factor.  (Appendix C lists all the
pulping and bleaching model process units used in the database
system, with the emission point-specific emission factors and
vent or stream characteristics.)  When these model process
units are merged with the pulp and paper mill database, an
industry characterization database is produced (made up of
model mills) with sufficient information to allow calculation
of uncontrolled air emissions.  Although this model
characterization is not an exact representation of each mill
in the industry, it is a reasonable characterization for
purposes of assessing the relative impacts of alternative
control options on the industry as a whole.
     As described in Chapter 2.0, the industry was also
characterized with regard to baseline air emission control
levels.  Information was gathered through guestionnaires and a
review of existing regulations to allow a determination of
which emission points are currently controlled for each mill
in the database.
     As described in Chapters 3.0, 4.0, and 5.0,  the data-
gathering efforts also identified applicable control' options
for the emission points identified.  For each control option,
procedures were developed to estimate the cost and
environmental impacts associated with the application of that
control to a specific emission point in a mill.  This input
control file was used in calculating the national impacts for
specified air control options.
6.2  CALCULATION OF NATIONAL EMISSIONS AND CONTROL IMPACTS
       Baseline air emissions were calculated from the
uncontrolled air emissions (i.e., model process unit emission
factors multiplied by mill-specific line capacities)  by
                              6-3
-------
assigning appropriate control efficiencies to the control
devices that were assumed to be present at each faci-lity.  The
uncontrolled and baseline emissions, calculated by emission
point, were then summed for each process line and mill.
National emissions were estimated by summing emissions from
all individual mills.
     National air control impacts (emissions, emissions
reductions, and costs) were calculated for each mill based on
a range of air control options.  The assumptions and
procedures for the impacts are given in Chapter 4.0
(Environmental Impacts) and Chapter 5.0 (Costs).  Taking into
account the baseline level of control assumed to be present at
each facility, controlled emissions were calculated for each
control option by emission point and were summed for each
line, for each mill, and for all mills combined.  Because the
add-on controls may be applied to multiple emission points
within a mill, control costs were not calculated by "emission
point; but instead were calculated by line or by mill.  That
is, depending on the capacity of the applicable control
device, multiple streams were assumed to be routed to the
device together (e.g., via a common header).
     Note that because some of the EPA Office of Water control
options include process modifications that change the model
process unit assigned to a mill, model process units were
reassigned to the specific mills.  After this reassignment
process, impacts of air control options are then estimated,
accounting for the process modifications.
6.3  GENERATION OF SUMMARY OUTPUT FILES
     As shown in Figure 6-1, the database system generates
output tables summarizing emissions, emissions reductions,
control costs, and electricity and fuel use.  The output files
for the proposal are in Reference 4.  These summary tables
also include the water control impacts provided by the EPA
Office of Water as an input to the database.  These output
tables include pollutant-specific air emissions and emissions
reductions for baseline and for each control option, as well
                              6-4
-------
as total capital and annual costs and secondary environmental
impacts.
                              6-5
-------
6.4  References
1.   Responses to the 1990 U.S. EPA National Census of Pulp,
     Paper, and Paperboard Manufacturing Facilities Section
     308 Questionnaire and Supplements (Confidential Business
     Information).  1992.

2.   1991 Lockwood-Post's Directory of the Pulp, Paper, and
     Allied Trades.  San Francisco, Miller Freeman
     Publications.  1990.   p. 9.

3.   Responses to Industry Survey discussed in the following
     letter:  J.E. Pinkerton, National Council of the Paper
     Industry for Air and Stream Improvement, Incorporated
     (NCASI), to J. Telander, EPA: 15B, and P. Lassiter, EPA:
     CPB.  February 11, 1992.   (Responses were claimed
     confidential business information).

4.   Memorandum from Olsen, T.R., and C. Reed, Radian
     Corporation, to Shedd, S.A., EPA/CPB.  Revised Integrated
     Database Outputs.  June 9, 1993.
                              6-6
-------
  APPENDIX A




FIELD TEST DATA
-------
                            APPENDIX A
                         FIELD TEST DATA

A.I  INTRODUCTION
     The EPA conducted a field test program to gather air
emissions and liquid sample data by which to characterize
emission sources within the pulp and paper industry.  The purpose
of the program was to obtain data that could be used as a basis
for a national emission standard and as a basis for developing
air pollution emission factors.  Specific objectives of the
testing program related to the national emission standard include
characterizing emissions and emission sources within the pulp and
paper industry and evaluating the effectiveness of various
controls under consideration by EPA for MACT.  Testing was
conducted at a total of five facilities including four kraft and
one sulphite mill.  One of the four kraft facilities also had a
neutral sulfite semi-chemical process which was sampled.  Testing
at each facility consisted of two parts:  (1) air emission
sampling of process vents on pulping and bleaching units, and (2)
sampling of liquid process fluids which consist of weak black
liquor, condensates, and wastewater.
     This appendix contains a summary of the results obtained
from the field sampling program.  Brief summaries of each field
test and the results obtained are presented in the following
sections.  Additional details regarding field test procedures and
results are available from individual test reports for each test
site.
     The information reported in this appendix are taken directly
from the field test reports and are in units of Ib/hr for gaseous
measurements and jug/mL for liquid measurements.  Conversion of
the measured values to units associated with production rate is
discussed in Appendix B.
A.2  TEST DATA
     A.2.1  Site 1.  Site 1 was selected for field testing
because it is considered to be representative of the kraft pulp

                               A-l
-------
 and paper  industry and  because  several  technologies that are
 potentially  MACT  for  the  process  are  in use  at the facility.
 Site  1  is  an integrated bleach  kraft  pulp mill.  The mill
 produces kraft  pulp from  both hardwood  and softwood chips.  The
 pulp  is used to produce uncoated,  white free-sheet paper for  copy
 machines,  manuals,  brochures, printing,  business forms, and
 envelopes.   The mill  also produces bleached  pine and hardwood
 market  pulp,  approximately 20 percent of which is in the form of
 baled pulp.   An overview  of the processes at the site  are
 presented  in Figure A-l.
      Sampling points  from Site  1  are  located in the pulping,
 chemical recovery,  and  bleaching  process areas of the  mill.
 Site  1  pulps both pine  (50 percent) and hardwood  (50 percent).
 Figures A-2  and A-3 present the hardwood and softwood  pulping
 processes.   Hardwood  chips are  cooked in one of two batch
 digester pulping  lines  and the  pine chips are cooked in one
 continuous digester.
      The hardwood pulping process consists of two batch digester
 lines and  two brownstock  washer lines which  combine to one
 screening  and oxygen  delignification  line  (see Figure  A-2).   Each
 batch digester  line contains six  batch  digesters operated  in
 parallel.  The  digesters  empty  to one of two blow tanks, one  for
 each  digestion  line.  The gases and steam are collected in a
 direct-contact  accumulator and  the pulp enters the washing line.
 The steam  and condensible gases are condensed in the direct-
 contact accumulator with  a portion of the cooled condensate  from
 the accumulator.   The noncondensible  gases  (NCG) from  the
 accumulator  are vented  to the NCG control system and are combined
 with  evaporator condensates from  chemical recovery and steam
 stripped.
      After the  blow tanks, hardwood pulp flows to a knotter  which
 removes undigested wood chips and returns them to the  digesters.
 The hardwood pulp is  then separated from the spent cooking
 chemicals, or black liquor, in  a  countercurrent,  3-stage
_brownstock washing system.  Each  stage  consists  of one vacuum
                                A-2
-------
   Hardwood
Hardwood
                                                   Softwood
           aaachlng
            cJf3T
                             \ Pap«f Making ]
Pigurar A-l.   GeneralProcess Diagram  for,Sit* l
                          A-3
-------
                                                                 0)
                                                                JJ
                                                                •H
                                                                c/i
                                                                 U)
                                                                 0!
                                                                 0
                                                                 0
                                                                •H
                                                                 a
                                                                p-4

                                                                a,
                                                                 0
                                                                 0

                                                                T3
                                                                X
                                                                (S
                                                                 I
                                                                 a>
                                                                 V4
                                                                 3
A-4
-------
                                                          0)
                                                          V)
                                                          V
                                                          0
                                                          0
                                                          c
                                                          •H
                                                          a
                                                          i—t

                                                          a.

                                                          T3
                                                          0
                                                          O

                                                          4-1
                                                          
-------
drum washer.  The pulp from the two hardwood lines is then
combined.  The combined pulp enters two parallel, primary
screens, to remove oversized particles such as uncooked chips,
and then enters the decker for thickening prior to oxygen
delignification.  In oxygen delignification, the pulp is treated
with oxygen in an alkaline solution under pressure to remove
additional lignin.  The contents of the oxygen delignification
tower are released to a lower pressure blow tank.  The pulp is
washed, pressed, and stored before being sent to the bleach
plants.  The weak black liquor is recovered from the first stage
washers and stored.
     The pine chips are digested in a Kamyr, continuous pulping
process  (see Figure A-3).  The continuous digester is a two-
vessel system in which pine chips are continuously fed into the
first vessel with white liquor.  The digestion process continues
as the pulp flows from the first vessel to the second.  The pulp
and the liquor mixture flow from the second vessel to a two stage
diffusion washer.  Pine pulp flows upward through the washer
tower countercurrent to down-flowing wash water recycled from the
decker in a 2-stage diffusion washer.  The weak black liquor is
removed by extraction screens in the washer and used in the
digester for washing and cooling.  After exiting the washer, the
pulp enters a storage tank prior to flowing through a screening
system to remove oversized particles such as undigested chips,
then a decker, to thicken and wash the pulp.  The pulp slurry
then enters an oxygen delignification tower for removal of
additional lignin.
     The chemical recovery process for Site 1 is presented in
Figure A-4.  The weak black liquor from the first stage in the
hardwood brownstock washer lines and the softwood pulp diffusion
washer are collected to recover the cooking chemicals in this
process.  Combined weak black liquors enter a storage tank, where
soap is skimmed from the surface and sent to tall oil recovery.
The weak black liquor is concentrated in two parallel multiple
effect evaporators.  Soap is also extracted midway through the
                               A-6
-------
2,


>,
s
       J1H-
Si-
   [ill
       I
                     m
                           II
                          iO?
                          ••9«
                           la
                                       !
                      1!
                                     !
                                                        3

                                                        s
                                           I ? T
                                             I
                                         i
                                    J-
                     •I   "^
                                                     S
                                                     o
                                                     u
                                                     0)
                                                              fl
                                                              u
                                                              --^

                                                              V

                                                              5
                 A-7
-------
evaporators.  The concentrated liquor is then combined and
combusted in two parallel recovery furnaces.  The offgases from
the evaporators are vented to an electrostatic precipitator
(ESP).   The smelt, which contains sodium carbonate (Na2CO3) and
sodium sulfide (Na2S),  from the combustion of the black liquor in
the furnaces is mixed with water in the dissolving tank to form
green liquor.  The green liquor is mixed with calcium oxide (CaO)
to form calcium hydroxide (Ca(OH)2) in the slaker.  This mixture
flows to the causticizer to form white liquor (NaOH and Na2S).
The white liquor is stored for reuse in the digestion process.
The CaC03, called lime mud,  is first washed in the mud washer,
then combusted in the lime kiln to recover CaO, which is reused
in the causticizing process.
     The evaporator system condensates form two streams, one with
a lower volume and high concentration of volatiles and a second
with a high volume and lower concentration of volatiles. The high
volume stream is recycled in the mill for various uses and the
low volume stream is combined with the accumulator condensates
from hardwood pulping and turpentine underflow from softwood
pulping to be steam stripped.  The stripper is charged with waste
steam from the Kamyr digesters.  The liquid stream exiting the
steam stripper is used as wash water for the second washer of the
oxygen delignification section.  The exiting vapor stream  is
condensed.  The noncondensible gases are sent to the lime kiln
and the condensate, consisting of primarily methanol and water,
is sent to a rectifier.
     The vapor exiting the rectifier consists primarily of
methanol and is routed to the lime kiln.  The water stream is
combined with the evaporator condensates and accumulator
condensates that enter the first steam stripper.
     Oxygen delignified pulp is bleached in one of two 3-stage
bleach lines.  Site 1 has one bleach line dedicated to hardwood
pulp and one line dedicated to softwood pulp.  The bleaching
lines are similar and presented in Figure A-5.  The 3-stage
sequence consists of chlorine/chlorine dioxide  (C/D) stage, an
                               A-8
-------
                                                             
-------
extraction with oxygen (Eo) stage, and a chlorine dioxide (D)
stage.  There are two differences between the two lines.  The
first difference is the bleaching capacity.  The hardwood line
has a 600 ton per day capacity and the pine has an 800 ton per
day capacity.  The second difference is the chlorine dioxide
substitution rate.  The chlorine dioxide substitution rate,  as
active chlorine, for the pine pulp line is 50 percent and is
15 percent for the hardwood pulp line.  After treatment in each
bleaching tower, the pulp is washed prior to entering the next
stage.  The wash water from the D-stage is recycled in the C/D
stage and Eo stage washers.  Filtrate from the C/D and Eo-stages
is sewered in the acid and caustic sewer, respectively.  The
bleached pulp is then stored in towers prior to use in paper
production.
     The objectives of the test program at this facility were to
characterize kraft hardwood digested pulp, kraft softwood
digested pulp and weak black liquor, kraft softwood oxygen
delignificaiton, kraft wastewater from both the pulping and
bleaching areas of the mill, kraft softwood bleaching with 50
percent chlorine dioxide substitution, and kraft hardwood
bleaching with 15 percent chlorine dioxide substitution.  Other
objectives were to quantify air emissions of total VOC and
several specific compounds of concern from process vents.
     Air emission tests were conducted at two locations in the
hardwood bleach plant and three locations in the softwood pulp
mills and bleach plant.  These are listed in Table A-l along with
the identifiers for each sampling location.  Several test methods
were used to measure emissions of the various constituents of
concern.  Table A-2 presents average emission rates for each
constituent of concern as measured at each of the five
measurement locations.  All measurement points and measurement
methods are identified in the table.
     Process liquid sampling was conducted in 6 different areas
of the facility.  Table A-3 identifies these areas and the points
at which samples were taken in each area.  The identifier for
                               A-10
-------
           Table  A-l.   Gas  Sampling Locations  at Site I

          	Location	                  Identifier

Hardwood Plant

     Vent into hardwood bleach plant scrubber          HV1
     Hardwood D stage vent/wash and tower seal tank    HV1A

Softwood Plant

     02  delignification blow tank  vent                  SV1
     Vent into bleach plant scrubber                   SV4
     Combined vent from EOwasher/filtrate tank         SV5
                               A-ll
-------
        Table A-2.'Measured Vent Emission Rates at Site l
                             (lb/hr)

COMPOUND
Acetone*
Acetone1*
Acrolein
MeK*
MeKb
Chloroform1*
Methanolb
HCLf
CL/
a-pinene*
B-pinene*
THCj
Measurement Points
SV1
0.0554
0.0912
NA
0.000567
0.0160
NA
2.16
NA
NA
0.116h
0.0617h
4.320
SV2
0.0784
0.00904
4.01E-4C
0.00296
6.29e-46
0.795
0.0747
0.0288
0.212
2.17e-6c
7.15e-5!
0.863
SV4
0.0124
0.01004
0.000441d
0.00289
1.82e-4e'
0.0435
0.0260
NA
NA
NA
NA
0.600
HV1
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
0.476
HV1A
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
0.377
a _

b _

c _

d _

e _

f _

g _
h _

i _

-j _

NA
Obtained using EPA Method 0011.
Obtained using NCASI Methanol method.
Value below detection limit of method.
Estimated value below calibration  limit.
Value below quantitation limit.
Obtained using EPA Method 26A.
Obtained using EPA Method 0010.
Estimated value above quantitation limit,
Estimated value below quantitation limit.
Obtained using EPA Method 25A.
- Not applicable
                               A-12
-------
 TABLE A-3.   Liquid Stream Sampling Locations at Site  1

	Location	                       Identifier

Softwood Bleach Plant
- Pulp into Cd tower                              SP5
- Pulp out of Cd tower                            SP6
- Pulp out of Eo tower                            SP7
- Pulp out of D tower                             SP8
- Pulp out of D washer                            SP9
- Wastewater from" bleach plant scrubber           WW6A&B
- Softwood acid sewer                             WW7
- Softwood caustic sewer                          WW8

Softwood O2  Delignification System
- Influent to delignification tower               SP3
- Pulp out of 02 delignification blow tank        SP4

Hardwood Bleach Plant
- Pulp out of Cd tower                            HP2
- Pulp out of Eo tower washer                     HP3

Softwood Diffusion Washer and Weak Black Liquor
- Pulp into diffusion washer                      SP1
- Weak black liquor                               SP2

Hardwood Vacuum Drum Washer
- Pulp into brownstock washer                     HP1

NCG System/Digester Condensates
- Hardwood accumulator condensates                WW1
- Combined evaporator (foul) condensates          WW2
- Turpentine decanter underflow                   WW3
- Turpentine storage underflow/
     NCG system condensates                       WW4
                          A-13
-------
each sampling point is also given.
     Liquid process samples were analyzed using high performance
liquid chromatography/gas chromatography (HPLC/GC) to quantify
pulping and bleaching compounds.  Some of the samples were also
analyzed using proposed Method 25D and proposed Method 305.
Table A-4 presents the average concentration of selected
compounds identified in the process stream samples.  Additional
details of the field sampling results can be found in the full
test reports.1'2
     A.2.2  Site 2.  Site 2 produces more than 2500 tons of paper
products, including creped paper, grocery bags, and corrugated
boxes.  Both kraft and neutral sulfite semi-chemical (NSSC)
pulping are practiced at this facility.  Approximately 2153 tons
per day of kraft pulp is produced exclusively from softwood and
approximately 144 tons per day of NSSC pulp is produced
exclusively from hardwood.  In addition, an old corrugated
container (OCC) plant produces pulp from bales of OCC purchased
from other sources.  An overview of the processes at the site are
presented in Figure A-6.
     Sampling points from Site 2 are located in the pulping and
bleaching process areas of the mill.  Figures A-7 and A-8 present
process flow diagrams of wood preparation and pulping for the
kraft and NSSC processes, respectively.  In the kraft process
(Figure A-7), screened chips and white liquor are added to 21
batch digesters and 2 Kamyr digesters, one of which operates with
a modified continuous cook.  The pulp from the batch digesters is
sent to five blow tanks.  Undersized chips and sawdust are cooked
with white liquor in three continuous sawdust digesters and
transferred to a common blow tank.  The pulp from all six blow
tanks is sent to brownstock washing, while the pulp in the Kamyr
digesters is washed within the Kamyr vessel and then sent to a
diffusion washer.
     In the NSSC digestion process  (Figure A-8), chips, sawdust
and pink liquor are cooked in two continuous digesters.  Pulp
                               A-14
-------
I
«
j  I

§  0.
3  C
     5!*
     S3S
     5 ° 5



     S3 S|||S
r § S 2 6 o
o o o v
          g 2 S
          o b *
     a r» n m en o M
     8 5 S 8 g g K
     O O O v V w
     SiSIiiS
                            a - s s si ss
                                                             if
                                                         lllll
                              A-15
-------
     H

     a
     o
                         'a.
                          o
                    (M
                    !i
                  ill
                  KflM
Figxir* A-6.  G«n«ral  Proc«a« Diagram for Site 2
                   A-16
-------
                                                         (N

                                                         0)
                                                         JJ
                                                         • H
                                                         cn
                                                         • H
                                                         a
                                                         rH
                                                         3
                                                         T3
                                                         C
                                                         o
                                                         fl
                                                         a
                                                         T3
                                                         O
                                                         O
                                                         9
                                                         U

                                                         §>
                                                        •H
                                                        Ch
A-17
-------
I       I
\
                                                           (N
                                                            c
                                                           •-4
                                                            a
                                                           r-i
                                                            3
                                                            (fl
                                                            U
                                                            •H
                                                            s
                                                            
-------
from the digesters is transferred to a common blow tank and then
sent to the screw presses for washing.
     The washing systems for both the kraft batch and continuous
pulp are shown in Figure A-9.  In the batch process, pulp from
the blow tanks is washed in 4-stage countercurrent brownstock
washing system.  In the continuous process, pulp from the Kamyr
digesters is washed in a 2-stage diffusion washer, screened, and
thickened in a decker.
     The NSSC washing process is presented in Figure A-10, where
screw presses are used to wash the NSSC pulp.  The NSSC pulp is
then transferred to primary refining, high-density storage,
secondary refining, low density storage, and finally to
corrugated medium production.
     In chemical recovery system at Site 2, weak black liquor
from brownstock washing and the Kamyr digesters is combined with
spent pink liquor from the NSSC screw presses, and sent to an
evaporation system to thicken the liquor.  After evaporation, a
portion of the black liquor is oxidized and then burned in the
recovery furnaces.  The remaining black liquor is sent to a
concentrator and then burned in the recovery furnaces.  Smelt
from the recovery furnaces flows into a dissolving tank where
filtrate from lime recovery dissolves the smelt to form green
liquor, and the dregs (impurities) are removed in a clarifier.
The clarified green liquor is mixed with lime in a slaker.  The
slurry formed in the slaker is agitated in a causticizing tank to
form white liquor and lime mud.  White liquor is removed from the
lime mud and is recycled for use in the kraft digesters.  The
lime mud is calcined in the lime kiln to make lime which is used
in the slakers.
     Condensible gases from the evaporators, digesters, and blow
tank vents are steam stripped and sewered, recycled to brownstock
washing or sent to lime recovery.  The overheads from the steam
stripper are vented to the turpentine recovery system.
Turpentine is decanted from the turpentine recovery condensibles
and the remaining liquid is routed back to the steam stripper.
                               A-19
-------
I
I

                                                                                                Oi

                                                                                                0)
                                                                                                *J
                                                                                                •^
                                                                                                VI
                                                                                                UJ
                                                                                                IB
3
Ck

JJ
-------
                    till
                                                  
-------
Noncondensible gases from turpentine recovery and the
evaporators, digesters, and blow tanks are sent to the NCG
collection system.
     The bleaching sequence at Site 2 is CEHD (chlorination with
approximately 5 to 40 percent chlorine dioxide substitution,
extraction, calcium hypochlorite, and chlorine dioxide).
Figure A-ll presents the flow through one of two similar bleach
plants at Site 2.  Fresh water is used as wash water for all of
the bleaching washers.  The chlorine tower and washer, the
chlorine dioxide tower and washer and the foam tower are vented
to a caustic scrubber.  The filtrates from the extraction and
hypochlorite washers are routed to the alkaline sewer.  The
chlorine and chlorine dioxide washer filtrates are routed to the
acid sewer.
     Objectives of the field tests at site 2 were to characterize
the compounds present in kraft weak black liquor, kraft digester
and blow tank offgas condensates, acid sewer, caustic sewer, and
bleach plant scrubber effluent.  Objectives also included
characterization of compounds present in and quantification of
air emissions from kraft bleaching with low chlorine dioxide
substitution, comparison of normal digestion to extended cook
digestion, and characterization of neutral sulfite semi-chemical
digestion.  Both process liquid and air emission samples were
collected and analyzed as a part of the program at site 2.
     Air emission tests were conducted at 4 locations at this
site: the E washer vent, the H tower vent, the H washer hood, and
the bleach plant scrubber inlet.  These sampling locations are
listed in Table A-5 along with the identifier for each location.
A summary of the average vent emissions of identified
constituents is given in Table A-6.
     Process stream samples were collected at a number of
locations throughout the plant.  Table A-7 lists the locations
and shows the identifier used for each location.  Sample analyses
consisted of a whole waste analysis using HPLC, GC/FID, and
GC/ECD.  The relative emission potential was measured using EPA
                               A-22
-------
        I;
^
i
    i
   OUJXO
   \
     III
            n<
           .« >
   -HI
   1-=
                   £'
    £**•--{
       -»>
                   O
,  i-q
I-T=:
      O
                                    U
                              Hi
                              S}X
~8
                           ur
                           H-jJ
                        »^
                        8
                          II
                               iJ
                                                   
-------
        Table A-5.  Gas  Sampling  Locations  at  Site  2

         Location	                  Identifier
E washer vent                                   V2
H tower vent                                    V3
H washer hood                                   V4
Bleach plant scrubber inlet*                    V5

Refer to Figure A-ll for details of the processes vented into
this scrubber.
                             A-24
-------
     Table A-6.
Summary of Average Vent Emissions at Site 2
            (lb/hr)

Constituent
Acetaldehyde*
Acetone*
Acetone"
Acrolein*
Chlorine0
Chlorined
Chlorine Dioxide*
Chloroform*1
Chloroform1"
Formaldehyde*
Hydrogen Chloride0
Methanol*
Methyl Ethyl Ketone*
Methyl Ethyl Ketone"
Methylene Chlorided
Methylene Chloride"
Pr op iona Idehy de*
Benzene"
Carbon Tetrachloride"
1, 1-Dichloroethane"
Chloromethane"
Toluene"
Bromodichloromethane"
a-Pinene"
p-Cymene"
-------
Table A-7.  Liquid Process Stream Sampling Locations at Site 2

	Location	                              Identifier

Weak black  liquor  from Kamyr digester                 PI
Pulp out  of Kamyr  digester                            P2a
Pulp out  of Kmyr digester - extended cook             P2b
Pulp into brownstock washer No. 7                     P3
Weak black  liquor  from brownstock washer N            P4
Soft pulp into  C & D washer                           P5
Pulp into C & D washer                                P6
Pulp into E washer                                   P7
Pulp into H washer                                   P8
Pulp out  of D washer                                  P9
Pulp into screw press                                 P10
Spent  liquor from  screen press                        Pll
Bleach plant scrubber wastewater                      WW1
Digester  &  blow tank off gas condensates              WW4
C  stage filtrate                                      WW5
                             A-26
-------
Method 25D.  Samples from some erf "the measurement points were
also analyzed for volatile organic compounds in accordance with
procedures in Method 8240 and for semivolatile organic compounds
in accordance with procedures in Method 8270.  Table A-8 presents
the results of the whole waste analysis and for the volatile and
semivolatile organic compound analyses.  Additional details of
the field test program at site 2 are available from the
individual test reports for the site.3'4
     A.2.3  Site 3.  Site 3 is a fully integrated kraft pulp and
paper mill.  Feedstock consists mainly of softwood chips.
Occasionally up to 10 percent hardwood is used.  The facility
produces 250 tons per day of bleached and semi-bleached kraft
market pulp and 1000 tons per day of kraft unbleached and
bleached linerboard, grocery bags, and saturated and converting
papers.  An overview of the processes at the site are presented
in Figure A-12.
     Sampling points from Site 3 are located in the pulping,
chemical recovery, and bleaching process areas of the mill.
Figure A-13 presents the process flow diagram for wood
preparation and digestion.  Softwood chips are fed into the
digesters along with white liquor.  Site 3 cooks their chips in
six batch digesters and two Kamyr continuous digesters.  One blow
tank serves all six batch digesters, while each Kamyr discharges
to a separate tank.  All the digesters vent to the turpentine
recovery system, while the blow tanks vent to condensers.  The
condensates are sewered and the noncondensibles are routed to a
vapor sphere.  The vapor sphere serves as a collection unit for
the noncondensible gas system and is expandable to handle
variations in gaseous flow.  Pulp and liquor separated from
digester gases in the blow tanks are then sent to the brownstock
washers.
     Figure A-14 presents the brownstock washing configuration at
Site 3.  Pulping liquor from the batch digesters is washed in a
three stage countercurrent vacuum washer (Washer No. 2).  Fresh
                              A-27
-------
I
CM
a
•
I
   c
   I
   4^
   0)
8  g
2
I
   01
      5 8 5 S S ' ' J 8 J
     000066    6
     696  66
             3 8 §
     b b b v b b   oi  o  b b
     b b b v b b   nboibbb  b  b  b  b  b
      S*WOQrt
     . o « 5 S S
     55*13188 ' 'S
      O  y
                  O   O
                          o  o   o
     5s  ,;  ;  ,J,«
     li
55
I"
             IS
         li
        S'
?ll
               «J-i   *,   li»*
                 x g s    ...  i •, _
                                                fi

           6 I 5 4 £ 5
                          i
                ill!
$e
                    fs i
      «|
ffjiitih
  A-28
                              s*
|!
tiiiiJm!
                                   .22.
                                                fljlj

                                                :^ « ' §
-------
6 Batch Digesters
3 Stage Vacuum
Pulp Washing
  Bleaching
Papermaking
                          Wood Preparation
  No. 4
  Washer
                              Pulp
                              Storage
Unbleached
Papermaking
                       2 Kamyr Digesters
3 Stage Vacuum
Pulp Washing
     Market Pulp
         Figure A-12.  General Process Diagram for Site 3
                              A-29
-------
                                                         0>
                                                         -U
                                                         0)
                                                         U)
                                                         Ul
                                                         
-------
I
n

-------
water is introduced at the third stage.  The filtrate tanks are
equipped with a foam tank to decrease the amount of foam in the
washer system.  Weak black liquor from stage one is sent to weak
black liquor storage for later chemical recovery.  Washed pulp is
thickened in a double decker before being sent to the high
density storage area.  Pulp and liquor from Kamyr No. 2 is sent
through a washing system identical to the pulp from the batch
digesters (Washer No. 3).  However, instead of applying fresh
water, evaporator condensate is used as wash water for Stage 3.
Washed pulp is then thickened in a decker and stored.  The
brownstock pulp is then used to make unbleached products.
     Pulp and liquor from the batch digesters and Kamyr No. 1 is
washed in the No. 4 washer.  As shown in Figure A-15, the No. 4
washer is a seven stage counter current flow system, with fresh
water being applied at stage seven.  This washer system is called
a chemiwasher.  Weak black liquor from the first stage filtrate
tank is sent to weak black liquor storage.  Pulp from the
chemiwasher is sent to storage where it may be sold as unbleached
market pulp or sent to the bleach plant.
     Figure A-16 presents a flow diagram of chemical recovery at
Site 3.  Weak black liquor from all wash stages is filtered,
stored, and sent through weak black liquor oxidation where some
sodium sulfide (Na2S) may be converted to sodium thiosulfate
(^28203).  From the oxidation system, the black liquor is sent
to the evaporators for removal of water.  In the newer part of
the plant, strong black liquor from the No. 1 and No. 2
evaporators (55 percent solids) is stored and then sent through
another oxidation system.  From black liquor oxidation, the
strong black liquor is sent to the No. 3 direct contact
evaporator (DCE) furnace to convert the sulfur compounds to
sulfide and to drive off the remaining water.  Strong black
liquor form the No. 4 evaporator set  (50 percent solids) is
concentrated to 63 percent solids, stored, and sent to the No. 4
indirect contact recovery furnaces.
                               A-32
-------
 •* £
a£2
•pWr
^SS
|1|
5 • v
2-x-S
                    t J
i
1


!
•3
A

t.
                     : *»

                     l
    II
    ii
                                 n

                                 V
                                 V
                                 •H
                                 CO
                                 01

                                 (0

                                 2

                                 ^
                                 0
                                 2
                                •H
                                b.
    A-33
-------
A-34
-------
     Smelt produced from combustion in the recovery furnaces is
sent through dissolving tanks where water is added to dissolve
the sodium salts.  This solution, called green liquor, is the
treated with calcium hydroxide (Ca(OH)2) to form sodium hydroxide
(NaOH).   The Ca(OH)2 is derived from combustion of the calcium
carbonate (CaCO3) precipitated from the causticizer in a lime
kiln to form lime (CaO), followed by the addition of water.
     In addition to the recovery of cooking chemicals, the
facility recovers turpentine from the digester vent, gases.  The
turpentine recovery system is presented in Figure A-17.
The digester vent gases are routed to a condenser.  The
noncondensibles along with overhead from the vapor sphere and the
evaporators are routed to the lime kilns.  Sulfamic turpentine is
decanted from the condensates.  The remaining condensates are
sewered.
     Figure A-18 presents a diagram of the bleaching process at
Site 3.   Brownstock pulp stored after being washed from Washer
No. 4 is pumped to the bleach plant where it is bleached in the
following sequence:
     •    Chlorine (Cl2) with approximately 85 percent chlorine
          dioxide (C102) substitution;
     •    Extraction with oxygen and peroxide; and
     •    Chlorine dioxide.
     Before the C12/C1O2 tower, a small amount of C1O2 is mixed
with brownstock pulp followed by further mixing with Cl2, and
more C1C>2 yielding 75 to 100 percent C1C<2 substitution.  From the
C12/C1C>2 tower, the pulp is washed and sent to the extraction
tower where oxygen and peroxide are added to dissolve the
residual lignin.  The pulp is then washed and sent to the C1O2
tower for additional bleaching.  After a final wash stage, the
bleached pulp is stored until needed for papermaking.  The
C12/C1O2 tower, all filtrate tanks, and all bleach wash stages
are vented to a caustic scrubber.  The extraction stage tower is
vented to the atmosphere.

                               A-35
-------
                                                0)
                                                CO


                                                -P
                                                m
                                                o
                                                o
                                                
-------
I
5
o
     *
 ,
5
ii
         5
       9
       ir
o
                     ii.
               X
                > a
             I
           D
              X
               X
             ! -
            r
ir
                *i


                a
                                             o
                                             o
                                             0
                14

                g.
                •H
                N
                  A-37
-------
     The objectives of the^Site 3 sampling program was to
characterize the compounds present in kraft softwood digested
pulp, weak black liquor, batch and continuous blow tank
condensates, turpentine underflow, evaporator condensates, acid
sewer, caustic sewer, and bleach plant scrubber effluent.  Other
objectives included characterizing the compounds present in and
quantification of air emissions from kraft softwood bleaching
with 85 to 95 percent chlorine dioxide substitution, comparison
of chemi-washing with conventional rotary vacuum washing and
quantification of air emissions from a brownstock washer foam
tank.  To achieve the objectives of the program, sampling points
at Site 3 were selected at locations in the pulping, chemical
recovery, and bleaching process areas of the mill.  Gas samples
were collected at two locations, the vent from washer no. 2 foam
tank and the vent into the bleach plant scrubber.  Gas sampling
locations and associated identifiers are shown in Table A-9.  The
results of the sampling at these locations is given in Table
A-10.
     Process liquid samples were taken at 18 locations in the
plant.  These are also shown in Table A-9 along with the
identifier for each sampling location.  Results from the analyses
of the process stream samples are summarized in Table A-ll.
Additional details of the testing at site 3 are available from
the detailed test reports for the site.5'6
     A.2.4  Site 4.  Site 4 is a bleached kraft pulp and paper
mill.  The mill pulps and bleaches hardwood and softwood
separately to produce a total of approximately 1850 tons per day
(TPD).  A pulp machine that runs either 100% hardwood or 100%
softwood, produces approximately 300 TPD of Food and Drug
Administration (FDA)-approved market pulp.  Two paper machines,
using varying blends of hardwood and softwood, produce
approximately 1550 TPD of paper.  Products include envelope
paper, photocopy paper, computer bond paper, and offset paper for
                               A-38
-------
    Table A-9.   Gas and Liquid Sampling Locations for Site 3

     	Location	               Identifier

Gas sampling locations

  Washer no. 2 foam tank vent                VI
  Vent into bleach plant scrubber"            V2

Liquid process stream sampling locations

  Pulp out of blow tank no. 1                SP1
  Pulp out of blow tank no. 3                SP2
  Weak black liquor form washer no. 2        SP3
  Pulp into chemiwasher no. 4                SP9
  Weak black liquor from chemiwasher no. 4   SP10
  Pulp into C12/CIO2 tower                    SP5
  Pulp out of CL2/CI02 tower                  SP6
  Pulp out of extraction tower               SP7
  Pulp out of CIO2 tower                     SP8
  Pulp out of D washer                       SP11
  Bleach plant scrubber effluent             WW1
  Blow tank condensates from batch digesters WW2A
  Blow tank condensates from kamyr digester  WW2B
  Turpentine underflow                       WW3
  No.  1 and 2 evaporator condensates         WW4
  Caustic sewer                              WW5
  Acid sewer                                 WW6
  No.  4 evaporator/concentrator condensates  WW7

  Refer to Figure A-18 for details on the processes vented into
the scrubber.
                               A-39
-------
       Table A-10.
Measured Vent Emission Rates at Site 3
         (Ib/hr)

Constituent
Acet aldehyde*
Acetone*
Acetone6
Acrolein*
Chlorine0
Chlorined
Chlorine dioxide4
Chloroform*1
Chloroform11
Formaldehyde*
Hydrogen chloride6
Methanol*
Methyl ethyl ketone*
Methyl ethyl ketone"
Methylene chloride*1
Methylene chloride6
Propionaldehyde*
Carbon tetrachlorideb
n-Hexaneb
Ch 1 or omethaneb
2-Butanoneb
Toluene"
Bromodichlororaethanef
Dibromochloromethanef
Dimethyl sulfide
Dimethyl disulfide
a-Pinene
b-Pinene
p-Cymene
p-Cymene
a-Pinene
b-Pinene
a-Terpinol
Total Hydrocarbons6
Measurement
VI |
0.098
0.316
0.043
—
NA
NA
NA
NA
—
0.003
NA
4.839
0.194
0.019
—
—
0.012
—
__
— —
0.019
— —
--
— —
0.920
0.249
1.376
0.508
0.058
0.256
6.471
0.970
0.110
27.306
Points
V2
0.001
0.001
0.004
0.005
0.041
1.112
6.648
0.235
0.045
0.002
0.011
2.265
0.009
0.000
0.042
0.001
0.001
0.002
0.001
0.049
0.000
0.001
0.004
0.001
—
— —
0.396
0.135
0.009
0.001
0.000
0.000
—
1.437
*  - Obtained  using Method  0011.
b  - Obtained  using Volatile Organic  Sampling Train.
0  - Obtained  using Method  26A.
d  - Obtained  using NCASI.
e  - Obtained  using 8240  analyses.
f  - Obtained  using Semivolatile Organic  Sampling Train.
 — Not analyzed
NA - Not applicable
                               A-40
-------
55
5
•t

I
   c

   'o
   Q.

   C
    ™ o. N is. N z   3




     ss83"as8 ' ' s
O  O i
8233:5
     S53SSS
     660666
                 ooo
     23
                                    666 66066666 6 6 6 oi  6
             s    s s
         !    .   S- *
         Ifsflfgils
                                  .    «„.   ..
                               [525jH$l??§t!i$i



                                A-41
                                                     ilili
                                                     i!??«
                                                     I Z • ^ o
-------
printing and writing.  An overview of processes at Site 4 are
presented in Figure A-19.
     Sampling points for Site 4 are located in the pulping,
chemical recovery, and bleaching process areas of the mill.
Site 4 processes hardwood and softwood chips in two separate, but
similar, lines.  Figure A-20 presents the wood preparation
pulping processes at the mill.  Logs are debarked and chipped and
stored in chip piles.  The chips are cooked with white liquor in
continuous Kamyr digesters to form pulp.  Noncondensible gases
(NCG) and pulp/liquor from the digesters are separated in a blow
tank and the pulp is screened to remove undigested fiber.  Black
liquor is washed from the pulp in brownstock washers and sent to
chemical recovery where it is converted back to white liquor for
reuse in cooking.
     The digester and blow tank off-gases are collected and sent
to a condenser.  The NCG's from the condenser are incinerated and
the condensates are steam stripped.  In the softwood line,
turpentine is recovered as a fraction from the condenser
receiving NCG from the digester, chip bin, and blow tank.
     Figures A-21 and A-22 present flow diagrams of hardwood and
softwood brownstock washing and oxygen delignification processes.
Hardwood pulp from screening enters a two stage countercurrent
brownstock washing system and then is routed to the oxygen
delignification tower.  Oxidized white liquor or caustic is added
to the discharge of the second stage washer.  A large portion of
the weak black liquor from brownstock washing is used as wash
water in the sections of diffusion washing in the Kamyr digester
and the remaining weak black liquor is sent directly to chemical
recovery.
      At the oxygen delignification tower more lignin is removed
from the pulp.  Pulp from the oxygen tower is washed in a two-
stage countercurrent rotary vacuum washer system.  Evaporator
condensates from chemical recovery are used as wash water for the
second stage.  A fraction of the filtrate from the first stage
                               A-42
-------
                      Log.
                                              Whftt
                                              Uquor
Figure A-19.   General Process Diagram for Site  4
                      A-43
-------
0«5 ?
t~l
3 1
, 	 , 2 *

- 1
I 1
t

,
if
12 ;
2«i' :
*ll|| :

?
5
11 	 3
Hi!
£4«|


j 	 la|j
«fl ?u.^(£
ol
rc

11




I ^
JL>
                                                     0)
                                                     .U
                                                     •H
                                                     CO
                                                     c
                                                     •H
                                                     a
                                                     r^
                                                     3
                                                     a.
                                                     C
                                                     0
                                                     Q,
                                                     0)
                                                     14
                                                     O4
                                                     O
                                                     o
                                                     CM
                                                      I
                                                     1)
                                                     hi
                                                     3
A-44
-------
                         art i
                   ill
                             c
                             o
                             • H
                             AJ
                             (0
                             O
                              C
                              Q)
                              X
                              O «
                               V
                              T3 •*
                              C W
                              cn
                              c
                              •H
                              £
                              a
                              «
                              0
                              0
                              «0
                              B
                              3
                              0»
                              •H
                              h
A-45
-------
                                                  c
                                                  0
                                                  u
                                                 •H
                                                 Q

                                                  C
                                                  0)
                                                  X 4)
                                                  O W
                                                    4J
                                                    fl
                                                  Ul
                                                  10
                                                  2

                                                  13
                                                  O
                                                  O
                                                  0
                                                  U)
                                                 (N
                                                 (N
                                                  I
A-46
-------
oxygen washer and filtrate from the presses are used as wash
water on the brownstock washer.
     The softwood line is similar to the hardwood line.  The only
differences are that the hardwood line contains two stages of
brownstock washing while the softwood line uses one stage and a
press;  In addition, pressate from the oxygen washers is recycled
as wash water on the second stage washer in the hardwood line,
while it is routed to the twin roll pressate tank on the softwood
line.
     Weak black liquor from diffusion washing and brownstock
washing is sent to chemical recovery.  Figure A-23 presents the
chemical recovery process at Site 4.  The weak black liquor
enters a multi-effect evaporator where the weak black liquor is
concentrated.  The hardwood line has a 6-effect evaporator, while
the softwood line has a 5-effect evaporator.  NCG's from the
evaporators are sent to a condenser.  NCG's from the condenser
are normally burned in an incinerator.  Clean evaporator
condensates are used for pulp washing.  Foul condensates are
steam stripped and the stripper effluent is then used for pulp
washing.  Other pulp mill foul condensates are also stripped in
this steam stripper.
     Strong black liquor from the evaporator is burned in a
recovery furnace.  Smelt form the recovery furnace is dissolved
in water to form green liquor and the dregs (impurities) are
removed by a clarifier.  The clarified green liquor is mixed with
lime in a slaker.  The slurry formed in the slaker is agitated in
a causticizing tank to form lime mud.  White liquor is removed
from the lime mud in a pressure filter and is reused in the
digester.  The lime mud is washed and burned in the lime kiln.
Quick lime produced in the lime kiln is reused in the slaker
process.  Gases from the lime kiln are scrubbed (No. 1 line) or
controlled with an electrostatic precipitator (No. 2 line).
     The bleaching sequence for the softwood line is C/D-Eo-D
(chlorine/chlorine dioxide, caustic extraction with oxygen and
chlorine dioxide).  Figure A-24 presents the flow through the
                               A-47
-------
                                                 T


                                                 0)


                                                 •H
                                                 0
                                                 u
                                                 0)
                                                 (X
                                                 0
                                                •H
                                                 s
                                                 flj

                                                g
                                                n

                                                 I
                                                <

                                                9)

                                                3
A-48
-------
                                                           0)
                                                          4J
                                                          •H
                                                          W

                                                          4J
                                                           fl

                                                          V)
                                                          w
                                                          01
                                                          o
                                                          0
                                                          tl
                                                          u
                                                          (0
                                                          01
                                                          rH
                                                          a

                                                          •o
                                                          0
                                                          o

                                                          4-1
                                                         
-------
softwood bleach plant.  Pulp from the second oxygen
delignification washer first enters the C/D tower and is followed
by a washer.  The washed pulp and some oxygen enters a caustic
extraction tower followed by a washer and then enters a chlorine
dioxide tower, followed by a washer.  Pulp from the D washer is
sent to a pulp machine or papermaking.  The chlorine dioxide
tower vents to a scrubber using water as the scrubbing medium.
     Fresh water is used on the D washer.  Filtrate from this
washer is used as wash water for both the caustic washer and the
C/D washer.  Filtrate from the caustic washer is sewered and used
as wash water for the C/D washer.  Filtrate from the C/D washer
is sewered.
     The bleaching process for the hardwood line is similar to
that for the softwood line and is presented in Figure A-25.  The
bleaching sequence is identical except that the caustic
extraction stage for the hardwood line does not use oxygen, the
hardwood D-stage washer sometimes uses pulp machine white water
as wash water, and the hardwood line bleach plant scrubber treats
the vent streams from all three sets of washers and seal tanks
and the chlorine dioxide tower.  White liquor is used as the
scrubbing medium.
     This test site was selected because it was considered to be
representative of the kraft pulp and paper industry and because
the mill uses technologies that might represent MACT for the
industry.  Specific objectives of the test program at this site
were to characterize kraft hardwood and softwood digested pulp
and weak black liquor, kraft hardwood and softwood bleaching with
chlorine dioxide substitution, screens/deknotters, and kraft
hardwood digester off-gas condensates, evaporator condensates,
acid sewer, caustic sewer, and bleach plant scrubber effluent.
Other objectives included quantification of air emissions from
kraft hardwood and softwood brownstock washers, and kraft
hardwood and softwood bleaching with chlorine dioxide
substitution.  Both process liquid and gaseous samples were taken
in the pulping and bleaching areas.
                               A-50
-------
I
                                                           0)
                                                           4-1
                                                           •^
                                                           C/3

                                                           4J
                                                           fl

                                                           Ul
                                                           10
                                                           0)
                                                           o
                                                           o
                                                           Ui
                                                           a,

                                                           a*
                                                           c
                                                           o

                                                           
-------
     Gas samples were taken at 6-locations*in the plant.  These
locations and their identifiers are listed in Table A-12.
Results of the gas sampling are summarized in Table A-13.
     Liquid process stream samples were collected at 8 locations
in the Hardwood processing area, at 6 locations in the softwood
processing area, and at 6 locations in the wastewater collection
and treatment area.  Liquid sampling locations are summarized
below in Table A-14.  A summary of the results of the liquid
process stream sampling is given in Table A-15.  Additional
details of the field test program at this site can be found in
the detailed test reports for the site.7'8
     A.2.5  Site 5.  Site 5 is an integrated bleached, magnesium-
based sulfite mill.  The mill produces bleached market dissolving
sulfite grade pulp and papergrade sulfite pulp.  Both pulp grades
are made from 100 percent hardwood and/or softwood chips.
Dissolving sulfite pulp comprises 88 percent of the mill
production with papergrade sulfite pulp making up the remaining
12 percent.  Pulps produced in the mill are used in photographic
paper, plastic molding compounds, diapers, and plastic laminates.
Average pulp production is approximately 410 metric tons per day,
or 145,000 metric tons per year.  An overview of the process at
Site 5 is presented in Figure A-26.
     Sampling points.for Site 5 are located in the pulping,
                                                           6
chemical recovery, and bleaching process areas of the mill.
Figure A-27 presents a process flow diagram for wood preparation
and digestion operations at Site 5.  Nine batch digesters are
operated in parallel and empty to one of four dump tanks.  The
off-gases from the dump tanks are routed to a water scrubber,
called the nuisance scrubber, where sulfur dioxide  (802) released
from the dump tank off-gas is scrubbed.
     Following the dump tanks, the cooked pulp enters a washing
system.  A flow diagram of the five stage washing process was
claimed by the mill to be confidential business information.9
The pulp is washed in a three stage countercurrent washer and
                               A-52
-------
          Table A-12.  Gas'Sampling Locations at Site 4

     	Location	             Identifier

Hardwood Plant

  Brownstock washer vent                     HV1
  Vent into bleach plant scrubber*            HV4

Softwood Plant

  Brownstock washer vent                     SV1
  C/D washer vent                            SV4
  E washer vent                              SV5
  E seal tank vent                           SV8

  Refer to Figure A-25 for details on the processes vented into
  the scrubber.
                               A-53
-------
           Table A-13.
Gas Sampling Results at Site 4
     (Ib/hr)

Compound
Acet aldehyde*
Acetone*
Acetone1*
Acrolein*
Chlorine6
Chlorined
Chlorine dioxide*
Chloroform"1
Chloroform1"
Formaldehyde*
Hydrogen chloride0
Methanol*
Methyl ethyl
ketone*
Methyl ethyl
ketoneb
Methylene chloride*1
Methylene chloride1*
Propionaldehyde*
Benzene1*
Chloromethaneb
2-Butanoneb
Styrene5
Tolueneb
Dimethyl sulfide"
Dimethyl disulfide1*
a-Pineneb
b-Pineneb
p-cyraeneb
Acetophenonef
Hexachlorocyclo
-pentadienef
Hexachloroethanef
a-Pinenef
b-Pinenef
a-Terpineolf
Total hydrocarbons*
Measurement Points
HV1
0.038
0.172
0.052
0.001
NA
NA
NA
NA
BDL
0.001
NA
6.234
0.079

0.094

NA
0.004
0.005


0.094
0.005
0 . 007
0.561
0.214
0.038
0.013





0.011
0.005
0.012
7.136
HV4
0.108
0.475
0.155
0.489
18.89
59.24
31.44
2.238
0.868
0.046
0.536
2.746
0.234

BDL

0.110
BDL
0.031

1.729









0.002

0.001



2.379
SV1
0.060
0.258
0.026
0.001
NA
NA
NA
NA
BDL
0.005
NA
3.823
0.102

0.008

NA
BDL
0.001
0.004

0.008


0.219
0.028
.0259
0.156
0.004
0.002



1.122
0.385
0.169
11.96
SV4
0.001
0.004
NA
0.001
0.019
0.035
0.044
0.748
NA
0.005
0.009
0.922
0.003

NA

0.008
NA
0.000

















0.654
SV5
0.005
0.045
na
0.015
0.003
0.032
0.235
0.306
NA
0.003
0.002
1.359
0.014

NA -

0.006
NA
0.000

















0.817
SV8
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA

NA

NA
NA
NA

















2.389
*  - Obtained using Method  0011
b  - Obtained using VOST
c  - Obtained using Method  26A
d  - Obtained using NCASI
6  - Obtained using Method  25A
f  - Obtained using SEMIVOST
NA - Not applicable     BDL - Below detection limit


                              A-54
-------
        Table A-14.   Liquid  Sampling Locations  at  Site  4

     	Location	                         Identifier

Hardwood Processing Area

  Pulp out of the blow tank                            HP1
  Weak black liquor from Kamyr digester                HP2
  Pulp into 1st stage brownstock washer                HP3
  Weak black liquor from 1st stage brownstock washer   HP4
  Pressate from 2nd stage brownstock washer            HP5
  Pulp out of 1st stage brownstock washer              HP6
  Pulp into C/D washer                                 HP8
  Pulp into E washer                                   HP9

Wastewater Processes

  Blow tank condensate                                 WW1
  Evaporator condensates to steam stripper             WW2
  Evaporator condensates to 02 delignification washer   WW3
  Acid sewer                                           WW4
  Caustic sewer                                        WW5
  Scrubber effluent                                    WW7

Softwood Processing Area

  Pulp into 1st stage brownstock washer                SP1
  Weak black liquor from 1st stage brownstock washer   SP2
  Pressate from press                                  SP3
  Pulp out of 1st stage brownstock washer              SP4
  Pulp into C/D washer                                 SP5
  Pulp into E washer                                   SP6
                               A-55
-------
!  I
"  E

|  2

«  u
J  (0
a  „
       S o 9 5 8 I I 9 9 «

      . *^ ""t  9 ^   T7 TT •"
      o o o  o «   v v
      01 O O O O -   V W
      55 6 «  b g -
      o o V «- 6 jp «-
      Ol O »- O O
IMili' ';;8


       1 '235
      60606
         9 £ § 3 £ ' ! ?
         ZSSwF'-r*:   ^
          6 « * W   w>
       *- « o o «
W 6 -  en
      ^ o ^ o o *-
      in A o» 6 6
      o o « o o
      o o «- 6 o a  o
               v ^
      oi o •*
       i S § i s s i' 'l
      <•) O O - W
      m o 9 o o
               ' ' §
      -   ^i   !=
        sslfS^l«1
           liii
         1
                   1-8
                   ,§;
                               A-56
-------
    p.
    i o
    y>
j CO
                  §5-
                             e
                             (0
                             U)
                             0)
                             0)
                             U
                             o
                             0)

                             0)
                             o
             VO
             
-------
                                                    in

                                                    d)
                                                    .p
                                                    •^
                                                    03

                                                    JJ
                                                    (0

                                                    OJ
                                                    W
                                                    (U
                                                    0
                                                    0
                                                    CTI
                                                    3
                                                    a>

                                                    T3
                                                    c
                                                    0
                                                    fl
                                                    a
                                                     0
                                                     0
                                                     V4
                                                     3
A-58
-------
temporarily stored in a soak tank for volume control to the
knotters system.  Spent cooking liquor (or weak red liquor) from
the first stage filtrate tank is sent to the evaporators.  The
pulp then passes to a knotter followed by a fourth washing stage.
The pulp passes through another screening system before being
thickened in the decker.  The washed pulp is sent to low density
storage prior to bleaching.
     The weak red liquor from washing is stored and sent to
chemical recovery.  Figure A-28 presents a flow diagram of the
chemical recovery process.  The spent liquor is concentrated in
the evaporator system.  Vapors expelled from the evaporator
system pass through a condenser system.  Noncondensible gases are
sent to the acid plant, while evaporator condensates are sewered.
The concentrated red liquor is combusted in a recovery furnace
where sulfur dioxide gas (802) is routed to the acid plant.  The
ash is slaked to recover the magnesium oxide, which is sent to
the acid plant.  The cooking liquor is produced in the acid
plants for use in digestion.
     The figure of the bleaching process used at Site 5 was
claimed as confidential and can be found in the CBI file (Refer
to Reference 9).  Brownstock pulp from low density storage is
usually bleached in a four stage bleaching sequence:  oxygen (O),
extraction (E), either peroxide (P) or hypochlorite (H), and
chlorine dioxide (D).  The peroxide/hypochlorite stage is
actually a series of 12 batch cells which can be run
independently as needed.  Pulp from the bleach plant is sent to
papermaking.
     Objectives of the field test at Site 5 were to characterize
the compounds present in sulfite digested pulp and weak black
liquor, sulfite bleaching, and in sulfite evaporator condensates,
bleach plant wastewater, and the paper machine white water.
Other objectives were to quantify air emissions from sulfite blow
gases and sulfite bleaching.  Both process liquid and air
emission samples were collected in the pulping and bleaching
                               A-59
-------
                     il
a
                                            4J

                                            fl
                                            u
                                            
                                            06
                                            (0
                                            u
                                            •H

                                            0)

                                            u
                                            00


                                             I






                                             3

                                            •H

                                            h.
A-60
-------
areas of the plant while processing both paper grade and
dissolving grade pulp.
     Air emissions were sampled at 7 locations within the plant.
These are identified in Table A-16.  The results of the air
emission testing are summarized in Table A-17 for the samples
collected while processing dissolving grade pulp and in Table A-
18 for the samples collected while processing paper grade pulp.
     Liquid process stream samples were collected at 16 locations
while processing both types of pulp.  Sampling locations are
identified in Table A-19.  The results of the analyses of these
samples are summarized in Table A-20 for both paper grade and
dissolving grade pulp.  Additional details of the field tests at
site 5 are available in the detailed test reports for the
site.10-11
                              A-61
-------
          Table A-16.  Gas Sampling Locations at Site 5

     	Location	                   Identifier

  Green stack1                                     VI
  Roof vent2                                       V2
  No.  2 (E stage)  combined seal tank vent         V3
  No.  2 A (E stage)  combined seal tank vent        V3A
  No.  3 seal tank vent                            V4
  Oxygen stage blow tank vent                     V7
  Nuisance scrubber inlet                         V8


1  This vent includes the C-stage tower, washer, and seal tank (no
  chlorine was added at the stage during the test), El-stage
  washer, P/H-stage tower and washer, and D-stage tower.

2  This vent includes the E2-stage washer and the D-stage washer.
                               A-62
-------
 Table A-17.
Gas Sampling Results at Site 5 - Dissolving Grade
            Pulp (Ib/hr)

Compound
Acet a Idehyde1
Acetone1
Acetoneb
Acrolein1
Chlorine6
Chlorine4
Chlorine dioxide4
Chloroform4
Chloroform1*
Forma Idehyde1
Hydrogen chloride0
Methanol1
Methyl ethyl ketone1
Methyl ethyl ketoneb
Methylene chloride4
Methylene chlorideb
Propiona Idehyde1
Chloroform1"
Chloromethane"
2-Butanoneb
Methylene chloride1"
Acetone6
a-Pineneb
p-Cymeneb
Hexachlorocyclo-
pentadienef
p-Cymenef
a-Pinenef
Total hydrocarbons6
Sampling Locations
VI ]
0.004
0.585
0.143
0.057
22.25
9.096
1.887
0.362
0.095
0.006
0.216
0.200
0.168
0.085
—
0.001
0.005
0.082
0.048
0.074
0.001
0.124
~
0.042
0.001

0.028
—
0.911
V2
0.009
0.240
NA
0.002
— —
—
—
0.103
NA
0.002
0.009
0.144
0.043
NA
0.016
NA
0.003











0.438
V4
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA











0.072
V7
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA











3.389
V8
0.051
0.027
0.000
0.000
NA
NA
NA
NA
—
0.000
NA
3.607
0.002
—
NA
0.001
0.003

0.027

0.007

0.002
0.258


0.343
0.001
2.708
1  - Obtained using Method  0011
b  - Obtained using VOST
c  - Obtained using Method  26A
d  - Obtained using NCASI
e  - Obtained using Method  25A
f  - Obtained using SEMIVOST
 — Not analyzed
NA - Not applicable
                               A-63
-------
 Table A-18.
Gas Sampling results at Site 5 - Paper Grade Pulp
               (lb/hr)

Compound
Acetaldehyde*
Acetone*
Acetone6
Acrolein1
Chlorine0
Chlorined
Chlorine dioxided
Chloroform*1
Chloroform1"
Formaldehyde*
Hydrogen chloride6
Methanol*
Methyl ethyl ketone*
Methyl ethyl ketoneb
Methylene chlorided
Methylene chloride6
Propionaldehydeb
Bromomethaneb
Chloromethaneb
Methylene chlorideb
Acetone15
1,2,3-
Tr i ch 1 or opr opaneb
a-Pineneb
b-Pineneb
p-Cymeneb
Hydroquinonef
p-Cymenef
a-Pinenef
b-Pinenef
Total hydrocarbons6
Measurement
VI
0.015
0.039
0.001
0.176
4.363
3.867
0.396
0.030
—
0.003
0.389
0.117
0.031
—
—
0.033
0.003


0.030
0.001






0.069
0.001

0.445
V2 -
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA













0.250
V3
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA













0.007
J^ V3A
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA













0.160
Locations
I V4 - |
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA













0.005

V7
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA













1.309

| V8
0.018
0.014
0.001
0.000
NA
NA
NA
NA
__
0.000
. NA
2.175
0.001
0.000
NA
— —
0.001
0.006
0.046

0.006
0.003

0.031
0.014
0.132
0.003
0.531
0.037
0.001
3.298 -
'  - Obtained using Method  0011
b  - Obtained using VOST
0  - Obtained using Method  26A
d  - Obtained using NCASI
6  - Obtained using Method  25A
f  - Obtained using SEMIVOST
 — Not analyzed
NA - Not applicable
                               A-64
-------
       Table A-19.   Liquid Sampling Locations at Site 5

   	Location	                    Identifier

Pulp into brownstock washer                     PI
Weak red liquor from 1st stage of brownstock    P2
Pulp into O2 tower                               P3
Pulp into E tower                               P4
Pulp into E washer                              P5
Pulp into D washer                              P6
Pulp into last cell of P/H tower                P7
Pulp into C/D washer                            P8
Pulp into C/D tower                             P9
Pulp into P/H tower                             P10
Pulp out of D washer                            Pll
Nuisance scrubber effluent                      WW1
Evaporator condensates                          WW2
Acid sewer                                      WW3
Caustic sewer                      .             WW4
White washer                                    WW5
                             A-65
-------

to
       o

       S.
1



I



(U
     M


     S
1
                   .
           »- o o v o o
              855i
              '-•r;z
                o
                V
                             • O • O

                            O v ° V
                                            1 '  i 8 9
                                               ^^
           fS8C8C''$8!5    I § §-3 8 8  ' '  i 8 i
           * r 9 *: ~      an*.-;-:"     z r,-
           — o g o o *dd*'        '
                                 o o o v v o
           UJOIlOGQOQQ {  1

           gPgHP^ZZ

           o v ° v v o
                      8 S S 8 8 8
                      r d r 6 d 9
                      O v ° V V °

                           SIX

                           d
                           v
                      ujdciv*"*"     civ
3K&S&il'S8n   5 n £
cpnpoooo    (otf>     (pola
ddno*"**      oi     tf>d<*i
                                                d
                                                v
           t 8 S S 2 S >
            v o o
           onnanoi  i r^ o *i    p cw o « o g  i
           ^Si5^S*"    8-     ^9S9B*
                                               o o
                                               V V
             o « o *- »•
           1089898    «8
           — qip^oiS    S>o

           *" O O y ° °      V
                                    d o
                                    v v
                                            i ICTOOO
                                             'nisi!:
           " d •«•' d d

                                 b — in y o
                           o
                           V
       i* d j- d — n
           fISiiiii  ' 'S
           o o — — o o
           o y n o o o
                                  d o» y *• *•
                                 3853288' '§85
                                 •1 "! •: d ^ ^      d
                                 « o 
-------
A.3  REFERENCES

1.   'Entropy Environmentalists, Inc.  Testing of Non-Combustion
     Processes in a Pulp and Paper Facility Site 1.  Data Summary
     Report.  Prepared for U.S. Environmental Protection Agency,
     Research Triangle Park, NC.  November 1992.

2.   Entropy Environmentalists, Inc.  Testing of Non-Combustion
     Processes in a Pulp and Paper Facility Site 1.  Draft.
     Prepared for U.S. Environmental Protection Agency, Research
     Triangle Park, NC.  August 1992.

3.   Roy F. Weston, Inc.  Field Test Data Summary for Site 2.
     Prepared for U.S. Environmental Protection Agency, Research
     Triangle Park, NC.  December 1992.

4.   Roy F. Weston, Inc.  Hazardous Air Pollutant Emission and
     Process Report Volumes I - IV Site 2.  Draft.  Prepared for
     U.S. Environmental Protection Agency, Research Triangle
     park, NC.  October 1992.

5.   Roy F. Weston, Inc.  Field Test Data Summary for Site 3.
     Prepared for U.S. Environmental Protection Agency, Research
     Triangle Park, NC.  December 1992.

6.   Roy F. Weston, Inc.  Hazardous Air Pollutant Emission and
     Process Report Volumes I - IV Site 3.  Draft.  Prepared for
     U.S. Environmental Protection Agency, Research Triangle
     Park, NC.  October 1992.

7.   Roy F. Weston.  Field Test Data Summary for Site 4.
     Prepared for U.S. Environmental Protection Agency, Research
     Triangle Park, NC.  December 1992.

8.   Roy F. Weston.  Hazardous Air Pollutant Emission and Process
     Report Volumes I - IV Site 4.  Draft.  Prepared for U.S.
     Environmental Protection Agency, Research Triangle Park, NC.
     September 1992.

9.   Trip Report.  Visits to Site 5 on May 15, 1991 and August
     20, 1991.

10.  Roy F. Weston.  Field Test Data Summary for Site 5.
     Prepared for U.S. Environmental Protection Agency, Research
     Triangle Park, NC.  December 1992.
                              A-67
-------
11.  Roy F. Western, Inc.  Hazardous Air Pollutant Emission and
     Process report Volumes I - iv site 5.  Draft.  Prepared for
     U.S. Environmental Protection Agency, Research Triangle
     Park, NC.  October 1992.*
     This information is located in the confidential files of the
     Director, Emission Standards Division, Office of Air Quality
     Planning and Standards, U.S. Environmental Protection
     Agency, Research Triangle Park, North Carolina 27711.  This
     information is confidential pending final review by the
     company and is not available for public inspection.
                               A-68
-------
                 APPENDIX B




AIR EMISSION ESTIMATES AND EMISSION FACTORS
-------
                           APPENDIX  B
           AIR EMISSION ESTIMATES AND EMISSION FACTORS

B.I  INTRODUCTION
     This appendix presents the methods by which air emission
factors from pulp and paper manufacturing processes were
estimated and presents the resulting air emission factors in a
series of tables.  The developed emission factors were based on
either the results from a sampling and analysis program at five
pulp and paper mills or on existing literature values.  Data from
the sampling and analysis program at five mills are presented in
Appendix A.
B.2  DISCUSSION
     Air emission factors were developed for a large number of
emission sources in the pulp and paper industry based on the
results of a test program at five different pulp and paper mills
involving both vent sampling and liquid measurements of process
materials.  Emission factors were calculated in units of grams of
air emissions per megagram of air dried pulp produced (g/Mg
pulp).  Several different procedures were used to calculate
emission factors depending on the type of emission source and the
types of data available for the source.  These procedures
included the following:
     •    Air emission factor calculations from the direct
          measurements at a tested vent.
     •    Air emission factor estimation based on the direct
          measurement of the composition of the liquid stream
          associated with the vent.
     •    Air emissions estimation from wastewater collection and
          treatment based on theoretical losses from model
          collection and treatment systems.
     •    Air emission factor estimates for black liquor storage
          tanks using a modification of the conventional storage
          tank emission equations.
-------
B.3  EMISSION FACTORS ESTIMATED FROM VENT MEASUREMENTS       3
     When the vent rate and chemical composition was measured for
a specific emission source or vent, an emission factor can be
estimated by dividing the mass emission rate of the vent  (grams
per day) by the mass flow rate of air dried pulp (megagrams or
metric tons per day) .  The units of the emission factor are
therefore grams of emissions per metric ton of air dried pulp
(g/Mg pulp) .
     The flow rates of pulp used in the calculations of emission
factors are based on reported plant production rates or on
typical operating conditions.
B.4  EMISSION FACTORS ESTIMATED FROM LIQUID MEASUREMENT
     When direct vent measurements are unavailable, liquid
measurements representative of the material being processed can
be used to theoretically estimate the air emission rate from the
units.  These theoretical estimates are based on equilibrium
partitioning of the volatile components between the liquid phase
and the gas phase.  Since the equilibrium partitioning factor
depends on temperature, a theoretical method was developed to
estimate the effect of temperature on the equilibrium
partitioning .
     Values of the Henry' s law constants from EPA' a compound
property data base were used as an estimate of the value  of the
partition coefficient in the process stream at a temperature of
25 °C.  This value of the partitioning coefficient may be
adjusted to represent other temperatures using the Antoines
Coefficients for each compound.
                        ~~ EXP
                                                           (2)
                               B-2
-------
where,
PT      »  Vapor pressure at temperature T  (mmHg).
T       =  Temperature  (°C).
A,B,C   =  Antoines Coefficients.
P2s     =  Vapor pressure at 25 oc.
     The values of A, B, and C are the Antoine's coefficients for
the vapor pressure correlation with temperature.  Equation  (I)
illustrates how the Antoine's coefficients can be used to
estimate the vapor pressure at any temperature and Equation  (2)
shows, the equation for a temperature of 25 °C.  Dividing equation
I by equation 2, yields the ratio of vapor pressure at
              _£l = EXP /-   B   +    B   \          (3)
              P25   **\   C + T    C * 25 '          l  '
temperature T to the vapor pressure at the reference temperature
of 25 °C.  This is illustrated in Equation  (3) .
     The value of the Henry's Law constant from the data base is
then adjusted by the vapor pressure ratio to obtain an estimate
of the Henry's law constant at the new temperature as follows:
                                 25 /

where,
HT   -  Henry's law constant at temperature T.
H25  -  Henry's law constant at 25 °C.

B.5 METHOD OF ESTIMATING THE PARTITION FRACTION  IN MIXED  TANKS
     When gas and liquid are mixed in a tank, some of the
volatile material in each of the two phases can  partition into
the other phase.  If chemical  equilibrium between the two phases
is achieved in the mixture  leaving the tank, the partitioning of
                               B-3
-------
the volatile components into the two phases can be described by
partition coefficients.
     The bleach plant/brownstock washer shown in Figure B-l can -
be used as an example of two-phase partitioning.  In this example
case, chloroform is emitted from the vent of the bleach plant
washer.  It is assumed that the concentration of chloroform is
unknown for both the process pulp liquid entering the washer and
for the entering spray.  It is also assumed that the
concentrations of chloroform in the pulp discharged from the
washer is known from sampling and analysis of the liquid leaving
the washer at the exiting pulp stream or at the recycle stream
produced from the washed pulp.  By assuming that the
concentration of chloroform in the liquid inside the washer is
the same as the concentration in the liquid leaving the washer,
emissions from the vent can be estimated using the ratio of the
volatilized component in the exiting vapor phase to the component
in the exiting liquid phase in conjunction with the Henry's law
constant.  This is illustrated below:
                     f _  mol vapor  _  „  G
                     A ~    1 7 .	r—; ~  nT —	
                         mol liquid     L p
                             liquid
where,
f    »  The  ratio  of  the  exiting  component  in the  gas  phase to
        the  component in  the  exiting  liquid.
HT   =  Henry's  law constant  at temperature T,  atm-m3/mol.
G    —  Gas  flow rate,  m3/s.
L    =  Liquid flow rate,  m3/s.
p    «  Atmospheric pressure  (assumed to be one atmosphere).
d<;   =»  Gas  density,  moles/m3.

The overall fraction of volatile material  in the entering process
liquid that exits with the gas is .estimated as follows:
                                B-4
-------
                          SV1
                       spray in
                pulp In
            SP1
           SP2-*
                                               SP3
                                SP4
                                       drain
                                        Q2C(1-fe]
Figure B-l.
Illustration of Air Emissions from a Bleach
Plant/Brownstock  Washer.
                                B-5
-------
                             F = —£_         (6)
                                 1 + f         V  '
where,
F    -  The  fraction of total volatile material  entering the
        reactor that exits in the gas phase.
     As a numerical example, assume that eleven grains per second
of chloroform enters a washer, one gram per second of chloroform
is vented from the washer, and the remaining chloroform exits
with the water  (10 grams per second).  The fraction in the vapor
is f =  1/10, or f = 0.1.  The fraction of the entering chloroform
that exits in the vapor phase is given by
          F = f / (1 + f) or F = 0.1 / (1+0.1)  or F = 1 /  11       (7)
An air emission factor can be estimated based on the unit
characteristics and the fraction of volat-iles lost  from the unit
using the following equation:
                             E = CL F L                         (8)


where,
E    *  Air emission factor  (g/Mg pulp).
CL   »  Concentration of the component in the liquid  (g/m3) .
F    =  Fraction of the component in the entering liquid phase
        that is emitted as air emissions.
L    -  Liquid flow rate (m3/Mg pulp).
     The  following example  illustrates the procedure for
calculating an air emission rate.   In  the EPA field test program,
liquid process stream samples were taken at the entrance of  a
bleach plant/brownstock washer  identified in Table  A-15 as

                                B-6
-------
Sampling Point SP1 at Site 4.1  The concentration of acetone in
these samples was determined to be 4.327 mg/L and the
concentration of pulp in the stream was determined to be  0.0163 g
pulp/g slurry.  The measured vent rate was 90.5 m3/Mg pulp.  In
this example, the concentration of acetone in the washer  is
estimated to be the same as the concentration in the inlet pulp
slurry.
     The molar volume of the gas exiting from the washer  vent is
calculated from the ideal gas law: 0.02887 m3/mol.  The volume of
liquid per Mg of dry pulp is calculated as I/. 0163, or 61 m3/Mg
pulp.  Using this information, the partition fraction of  acetone
in the washer may be estimated from Equation  (5) above as
follows:
                                 90.5
                                 61.4  0.02887
where,
f = HT £ dG = 0.000169 4^4 „ .L^ = 0.0086       (9)
f    =»  Ratio of the exiting component in the gas phase to the
        component in the exiting liquid.
HT   »  Henry's Law constant,  0.000169 atm-m3/mol.
G/L  =  Ratio of gas flow rate to the liquid flow rate,
        90.5/61.4 m3 gas/m3  liquid.
dg   =  Gas density, 1/0.02887 moles/m3.

     The overall fraction of the entering acetone that exits  with
the gas is estimated using  Equation  (6)  as  follows:

                               °-0086   =0.00857             (10)
                             1 + 0.0086


     The air emission factor for acetone can now be  estimated
from the unit characteristics and the fraction lost  from the  unit
using Equation  (8):
         E = CL F L  = 4.327 x 0.00857 x 61.3 = 2.27 g/Mg pulp    (11)

where,
                               B-7
-------
E    = Air  emission  factor,-2.27  g/Mg pulp.
CL   - Concentration of  the  component in  the  liquid,  4.327 g/m3.
F    = The  fraction  of the component  in the entering liquid
       phase  that  is emitted as air emissions,  0.00857.
L    = liquid flow rate,  61.3 m3/Mg pulp.
B.6  COMPARISON OF ESTIMATED AIR EMISSIONS FROM LIQUID
     CONCENTRATIONS
     Emission estimates based on direct measurement of vent gas
samples are generally the most accurate means of calculating
emission factors.  However,  in situations where no gas sampling
data are available, emission estimates based on measured
constituent concentraitons in the liquid process streams from
which the vent gases evaporate can produce reasonable emission
factor estimates.  This is illustrated by the information  in
Table B-l, which contains air emission estimates based on
information obtained from Site 4 of the EPA field test program.
The table contains estimates of emissions based on both gas
samples from test point SVI,  a bleach plant/brownstock washer
vent in the softwood plant,  and liquid samples of the process
streams in the bleach plant/brownstock washer (Test Points SP1,
SP2, SP3, and SP4).  As can be seen,  air emissions estimated from
the liquid concentrations are relatively consistent with the
estimates based on vent sampling for most of the sampling  points.
Liquid sampling would be expected to produce valid emission
estimates if accurate data are obtained for:
     • constituent concentrations in  the  liquid,
     • liquid and gas flow rates,
     • liquid temperature, and
     • Henry's law constants.
B.7  ESTIMATION OF AIR EMISSIONS FROM MATERIAL BALANCES
     If data from,  sampling and analysis are unavailable for both
vent gases and liquid process  streams, there  are some situations
where a material balanqe might be used to estimate emission
                               B-8
-------
rates.  Examples where this approach might yield valid results

would include situations where a large fraction of the volatile

   TABLE B-l.   SAMPLES COLLECTED AT A BLEACH PLANT/BROWNSTOCK
                             WASHER1
Compound
Acetone*
Methyl ethyl
ketone
Methanol
Type of sample
Inlet or outlet
Air emission factors (g/Mg pulp)
SVla
3.04
1.2
45
VENT
OUT
SPlb
2.27
1.22
146
PULP
IN
SP2b
2.51
1.46
147
WATER
OUT
SP3b
1.67
1.178
125
WATER
IN
SP4b,c
7.82
93
34
PULP
OUT
a The values of the air emission factors for the vent are
  obtained from the reported emission rate (Ib/hr, Table A-13)
  divided by the pulp rate (0.0849 million Ib air dried pulp/hr)

b These values were estimated from process liquid measurements
  reported in Table A-15, using procedures described in the
  preceding text.

c The results from this sample point are inconsistent with the
  other sample points presented in this table.
                               B-9
-------
components of a stream is released to the air.  In cases where-
the fraction of volatiles released to the air is low or is at or
below the detection limits of available test methods, a material
balance approach would not be expected to generate valid data.
B.8  MODEL WASTEWATER PLANT PARAMETERS
     In developing emissions factors for wastewater collection
and treatment units, EPA used the procedures described above and
an example model wastewater collection and treatment system.  The
characteristics of the model system used for the estimates are
described in Tables B-2 and B-3.  Table B-2 presents the assumed
waste stream flow rates and Table B-3 lists the elements within
the model wastewater collection and treatment system.
     The Agency is currently revising the model wastewater
collection and treatment system and anticipates the emission
factors presented here will change.
B.9  ESTIMATION OF AIR EMISSIONS FROM WASTEWATER COLLECTION AND
     TREATMENT SYSTEMS
     Emission factors for wastewater collection and treatment
systems at pulp and paper plants were calculated based on
measured concentrations of pollutants in the wastewater streams
together with the mass flow rate of the streams.  The total
fraction of volatiles emitted from a system was estimated by
summing the estimated emissions from each collection system
element using the following equation.

                         F* = £'^  f*< fo^                    <12>

where,
Ft       = Total  fraction of a  constituent  emitted  to the  air
           from the collection  and/or treatment system.
fei      = Fraction of a constituent emitted to the air  in
           unit i.
^o(i-i)   ™ Fraction of the  initial  constituent  concentration
           that remains  in  the  waste entering unit  i.
                               B-10
-------
TABLE B-2.  MODEL  PLANT FLOW RATES OF WASTE STREAMS2
Waste stream
acid wastewater
caustic wastewater
digester wastewater
clean condensates
foul condensates
turpentine
underflow
continuous blow
condensates
blow tank
condensates
weak black liquor
scrubber effluent
other
location
bleach plant C or CD washer
bleach plant E washer
pulping
evaporator
evaporator
pulping gas condensates
pulping
pulping
storage tank for treatment,
recycle to pulping
bleach plant scrubber
bypass clarifier, sent
directly to aeration basin
m3/Mg pulp
15
13
1..2
6
7
0.16
1
2
11
0.06
12
                         B-ll
-------
  TABLE B-4.   MODEL PLANT SEQUENCE OF COLLECTION SYSTEM
               ELEMENTS AND TREATMENT SYSTEM ELEMENTS.3'3
Name of unit
Trench
Drains
Junction box
Collection main
Junction box
Collection main
Clarifier
Aerated impoundment
Non aerated impoundment
Model for calculations
trench
equilibrium headspace,
collection system models
aerated impoundment, Chemdat?
manhole cover venting
aerated impoundment, Chemdat?
manhole cover venting
clarifier, Water?
aerated impoundment, Chemdat 7
non aerated impoundment,
Chemdat?
a  This  table  presents  the basis for the estimation of the
   emission factors from wastewater collection and treatment
                               B-12
-------
n         »  Total  number of units  in the  wastewater collection
             and/or treatment system.
     If air emissions are the only source of loss of a
constituent from a waste stream, the fraction of volatiles that
remain in the waste stream leaving a unit is equal to the product
of the fraction of volatiles in the waste stream entering the
unit and one minus the fraction emitted in the unit.

                        fo, = £0l.,(  1 - *.,)                     (13)
where,
foi  =  the fraction of  volatiles  in  the waste  stream leaving a
        wastewater  collection or treatment unit.

     When volatiles are lost from a waste stream by mechanisms
other than the air emissions, such as biodegradation and
adsorption, these other mechanisms must be accounted for in  the
calculation of the fraction of volatiles in the waste stream
leaving the unit.
     Once the total fraction of constituent emitted from a
wastewater collection and/or treatment system is calculated, an
emission factor for the system can be estimated as follows:
                 Efl   ?	)
                  f \Mgpulpj
where,
Ef « Emission factor.
Q  » The wastewater flow rate.
C  » Concentration of volatiles.
Ft » the total fraction emitted.
     Several example calculations of emission factors for
wastewater collection and treatment units can be found in
Reference 4.
                               B-13
-------
B.10 ESTIMATION OF AIR EMISSIONS FROM BLACK LIQUOR STORAGE TANKS "
     Weak black liquor is generated during pulping operations at
an estimated rate of 11 m3 per Mg dry pulp.5   This  wastewater is
normally collected in large storage tanks which are equipped with
vents which can release substantial quantities of air emissions
due to changes in the liquid level in the tank and to atmospheric
conditions.  The tank in the model unit has a conical roof with a
large central vent.6  No emission measurements were available for
this source and it thus became necessary to develop a theoretical
approach to estimating emission rates from these sources.   During
use, the wastewater level in the tank is more constant than the
working rate of liquid exchange would suggest, thus, it is not
realistic to assume that the quantity of gas emitted from the
vent would be equal to the working rate of liquid exchange.
Furthermore, there will be vent flow due to wind effects and due
to the stack effect created by warm moist air in the tank, which
would tend to make the vent rate greater than the contribution
from working losses alone.  It is also uncertain whether
equilibrium between the liquid and gas phase will be achieved in
the storage tank, especially for the larger vent rates, which is
a further consideration in the selection of the vent rate.
Considering all of these factors, it was assumed that saturated
vapors would be emitted at a rate equal to half of the working
rate of liquid exchange.
     Table B-4 lists a set of emission factors for storage tanks
containing black liquor.  The emission factor values are
primarily determined by the volatility of each individual
compound.
                               B-14
-------
Table B-4.  AIR EMISSION FACTORS  FOR BLACK LIQUOR STORAGE TANKS
Compound
acetone
2-butanone (MEK)
methanol
acrolein
acetaldehyde
alpha pinene
beta pinene
a-terpineol
chloroform
methylene chloride
formaldehyde
dimethyl sulfide
dimethyl disulfide
di chl or o t hi ophene
dichloroacetonitrile
toluene
chl orome thane
p cymene
proprionaldehyde
111 trichloroethane
Fraction emitted as air
emissions
0.001
0.003
0.000
0.002
0.002
0.055
0.039
0.010
0.065
0.061
0.001
0.100
0.041
0.017
0.007
0.120
0.143
0.254
0.001
0.261
                              B-15
-------
B.ll SELECTION OF EMISSION FACTORS-	
     Emission factors were developed for a large number of
sources in the pulp and paper industry.  For many of these
sources, emission factors were calculated in more than one way
resulting in multiple -values -for some constituents.
Additionally, emission factors for some of the sources have been
previously estimated by others and are available in existing
literature sources.  Under these circumstances, the goal of the
Agency was to select the emission factor value that best
represents actual emissions.  To assist in achieving this goal, a
protocol was established to determine the most appropriate
emission factor value to use for the source with multiple
estimates of emission factors available.  The established
protocol takes into account the type of source tests performed,
the test methods used, quality control measures taken, adequacy
of the test procedures and test documentation, and the
consistency of test results.  Table B-6 lists the considerations
used in selecting an emission factor from the available data.
     The beach plant/brownstock washer illustrated in Figure B-l
can be used as an example of a typical procedure for selecting an
emission factor when multiple estimates are available.  For this
example, acetone emission factor estimates were made for two
liquid samples at site 3 and for 4 liquid samples and 1 vent
sample at site 4.  These estimates were compared with the
emission factor available from the literature as shown in
Table B-6.  Examination of these data  indicate that the emission
factor estimate available in the literature is reasonably
consistent with the test results from  Site 3 but not with the
test results from Site 4 where the concentration of acetone in
the pulp was almost an order of magnitude lower than at site  3.
Because of the relatively good agreement between the literature
value and the results obtained for Site 3 for both liquid and
vent samples, it was concluded that the most appropriate action
was to  retain the existing  literature  value without change.
                               B-16
-------
TABLE B-5.
CONSIDERATIONS  IN  SELECTING EMISSION FACTORS.
(LISTED IN ORDER OF IMPORTANCE)
1
2
3
4
5
6
7
Quality of documentation and quality control procedures
for on-site sampling.
Type of test reported. Vent measurements of emissions
are preferred to estimations of vent emissions from
liquid measurements .
Source characterization and documentation.
Representativeness of the source.
Number of compound analyses included in the field test .
Consistency with other measurements and related sources
(Is the data point an outlier?) .
Conflicts between two different test methods of
reported measurements for the same compound are
resolved by selecting the higher measurement if there
is reason to believe that there is incomplete compound
recovery for the lower measurement .
                            B-17
-------
TABLE B-6. EMISSION FACTOR SELECTION FOR ACETONE  EMISSION FROM
           A SOFTWOOD BLEACH PLANT/BROWNSTOCK WASHER.
Sample
Identification
SP3
SV1
SP1
SP2
SP3
SP4
SP1
Test Site
3
4
4
4
4
4
3
Sample
Type
Liquid
Vent
Liquid
Liquid
Liquid
Liquid
Liquid
Emission factor from literature
Selected emission factor
Calculated Emission
Factor
(g/Mg dry pulp)
27
3.04
2.27
2.51
1.67
7.82
38
33
33
                               B-18
-------
Procedures similar to this were used in the selection of each of
the emission factors presented in the following discussion.
     Table B-7 contains a list of 237 individual sources used to
characterize model plants for the pulp and paper industry.  A
typical pulp and paper process unit would be expected to contain
some subset of the individual sources described in Table B-7.
The table contains a description of each individual source, an
identifying number, i.e., an "EP Code", for each source, the type
of pulp used as the basis for an emission factor (i.e., hardwood
or softwood), and the mill process involved (e.g.,  pulping,
bleaching).  For each individual source listed, the table also
identifies the source of information that served as the basis for
estimating the emission factor or describes how the emission
factor was estimated in the absence of source measurements.
     Sources of information utilized as a basis for emission
factors included both field test data and .data from existing
literature sources.  Data were not found for all of the emission
sources, which led to the use of alternative approaches to
estimate emission factors for these sources.  Several such
alternatives were developed.
     One approach was to assume that the emission factor for a
source with no data was the same as the emission factor for
another source with data if the emissions characteristics of the
two sources were judged to be very nearly the same.  Another
approach was to establish a series of factors to relate the
emission factor values from one set of emission sources to
another set of sources.  For example, data for emission sources
for which data are available while processing both softwood and
hardwood were used to establish a hardwood/softwood ratio.  That
ratio was then used to estimate emission factors for sources when
data were only available for one category of wood.   Another
approach was to establish a set of factors to show the relative
rate of emissions from individual units in series that
sequentially handle a product stream.  These factors were used to
                               B-19
-------
TABLE B-7.  EMISSION SOURCES AND "DATA SOURCES
EP
Code
1
2
3
4
7
8
9
10
13
14
15
16
17
18
19
20
21
Wood
Type
H
S
H
S
H
S
H
S
H
S
H
S
H
S
H
S
H
Mill
Process
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Emission Point
Description
chlorine dioxide
generation
chlorine dioxide
generation
C-stage tower vent
C- stage tower vent
C-stage acid sewer
C-stage acid sewer
bleaching effluent
bleaching effluent
bleach plant vents
bleach plant vents
fugitives from C12 use
fugitives from C12 use
H-stage (0.1-<0.5%) vent
H-stage (0.1-<0.5%) vent
H-stage (0.5-2%) tower
vent
H-stage (0.5-2%) tower
vent
H-stage (<0.5%) vent
Basis for
Emission Factor
Not used in Model
Plants
Not used. in Model
Plants
Extrapolated3 from
EP Code 71
Extrapolated from
EP Code 72
Ratioedb from EP
Code 8
Assumed same as
EP Code 40
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Assumed same as
EP Code 19
Assumed same as
EP Code 20
Extrapolated from
EP Code 151
Extrapolated from
EP Code 152
Not used in Model
Plants
                     B-20
-------
TABLE B-7.  EMISSIONS SOURCES AND DATA FACTORS  (CONTINUED)
EP
Code
22
23
24
25
26
27
28
29
30
31
32
33
34
35
36
37
38
Wood
Type
S
H
S
H
S
H
S
H
S
H
S
H
S
H
S
H
S
Mill
Process
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Emission Point
Description
H-stage (<0.5%) vent
H-stage (>2%) vent
H-stage (>2%) vent
no H-stage use, vent
no H-stage use, vent
H-stage (0.1-<0.5%)
wastewater
H-stage (0.1-<0.5%)
wastewater
H-stage (0.5-2%)
effluent
H-stage (0.5-2%)
effluent
H-stage (<0.5%)
wastewater
H-stage (<0.5%)
wastewater
H-stage (>2%) wastewater
H-stage (>2%) wastewater
no H-stage use,
wastewater
no H-stage use,
wastewater
bleaching effluent
w/slimacide
bleaching effluent
w/slimacide
Basis for
Emission Factor
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
Not used in Model
Plants
                           B-21
-------
TABLE B-7.  EMISSIONS  SOURCES  AND  DATA FACTORS (CONTINUED)
EP
Code
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
Wood
Type
H
S
H
S
H
S
H
S
H
S
H
S
H
S
H
S
H
Mill
Process
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Emission Point
Description
C1O2 subst. (0%) acid
sewer
C102 subst. (0%) acid
sewer
C1O2 subst. (0%) caustic
sewer
C1O2 subst. (0%) caustic
sewer
C1O2 subst. (0%)
effluent
C1O2 subst. (0%)
effluent
C102 subst. (0%) tower
vent
C1O2 subst. (0%) tower
vent
C1O2 subst. (100%) acid
sewer
C1O2 subst. (100%) acid
sewer
C1O2 subst. (100%)
caustic sewer
C1O2 subst. (100%)
caustic sewer
C102 subst. (100%)
effluent
C102 subst. (100%)
effluent
C102 subst. (100%) tower
vent
C102 subst. (100%) tower
vent
C102 subst. (high) acid
sewer
Basis for
Emission Factor
Ratioed from EP
Code 40
Site 5 (P3 DG, P4
DGd, WW3 DG)
Ratioed from EP
Code 42
Site 5 (P5-DG,
WW4 DG)
Not used in Model
Plants
Not used in Model
Plants
Extrapolated from
EP Code 75
Extrapolated from
EP Code 76
Assumed the same
as EP Code 55
Assumed the same
as EP Code 56
Assumed the same
as EP Code 57
Assumed the same
as EP Code 58
Not used in Model
Plants
Not used in Model
Plants
Extrapolated from
EP Code 79
Extrapolated from
EP Code 80
Ratioed from EP
Code 56
                            B-22
-------
TABLE B-7.  EMISSIONS SOURCES AND DATA FACTORS  (CONTINUED)
EP
Code
56
57
58
59
60
61
62
63
64
65
66
67
68
69
70
71
Wood
Type
S
H
S
H
S
H
S
H
S
H
S
H
S
H
S
H
Mill
Process
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Emission Point
Description
C102 subst. (high) acid
sewer
C102 subst. (high)
caustic sewer
C102 subst. (high)
caustic sewer
C102 subst. (high)
effluent
C102 subst. (high)
effluent
C1O2 subst. (high) tower
vent
C102 subst . (high) tower
vent
C102 subst. (low) acid
sewer
C102 subst. (low) acid
sewer
C1O2 subst. (low)
caustic sewer
C102 subst. (low)
caustic sewer
C102 subst. (low)
effluent
C102 subst. (low)
effluent
C1O2 subst. (low) tower
vent
C1O2 subst. (low) tower
vent
C- stage washer vent
Basis for
Emission Factor
Site 3 (SP6, WW6)
Ratioed from EP
Code 58
Site 3 (SP7, WW5)
Not used in Model
Plants
Not used in Model
Plants
Extrapolated from
EP Code 83
Extrapolated from
EP Code 84
Site 1 (HP2) ,
Site 4 (WW4)
Site 2 (WW5, P6) ,
Site 4 (SP5) ,
Site 1 (SP61,
WW7)
Site 4 (WW5) ,
Site 1 (HP 3)
Site 2 (WW6, P7) ,
Site 4 (SP6) ,
Site 1 (SP71,
WW8)
Not used in Model
Plants
Not used in Model
Plants
Extrapolated from
EP Code 87
Extrapolated from
EP Code 88
Assumed the same
as EP Code 87
                            B-23
-------
TABLE B-7.  EMISSIONS.SOURCES AND DATA FACTORS '(CONTINUED)
EP
Code
72
73
74
• 75
76
77
78
79
80
81
82
83
84
85
86
87
88
Wood
Type
S
H
S
H
S
S
H
H
S
H
S
H
S
H
S
H
S
Mill
Process
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Emission Point
Description
C-stage washer vent
C- stage seal tank vent
C-stage seal tank vent
C102 subst. (0%) washer
vent
C102 subst. (0%) washer
vent
C1O2 subst. (0%) seal
tank vent
C102 subst. (0%) seal
tank vent
C1O2 subst. (100%)
washer vent
C102 subst. (100%)
washer vent
C102 subst. (100%) seal
tank vent
C102 subst. (100%) seal
tank vent
C1O2 subst. (high)
washer vent
C102 subst. (high)
washer vent
C102 subst. (high) seal
tank vent
C102 subst. (high) seal
tank vent
C102 subst. (low) washer
vent
C102 subst. (low) washer
vent
Basis for
Emission Factor
Assumed the same
as EP Code 88
Extrapolated from
EP Code 71
Extrapolated from
EP Code 72
Assumed the same
as EP Code 87
Assumed the same
as EP Code 88
Extrapolated from
EP Code 76
Extrapolated from
EP Code 75
Assumed the same
as EP Code 83
Assumed the same
as EP Code 84
Extrapolated from
EP Code 79
Extrapolated from
EP Code 80
Site 4 (HP8, WW4)
Site 4 (SV4) ,
Site 1 (SP5, SP6)
Extrapolated from
EP Code 83
Extrapolated from
EP Code 84
Site 1 (HP2)
Site 1 (SP6) ,
Site 2 (P6) ,
Site 4 (SP5)
                            B-24
-------
TABLE B-7.  EMISSIONS SOURCES AND DATA FACTORS  (CONTINUED)
EP
Code
89
90
91
92
93
94
95
96
97
98
99
100
101
102
103
104
105
Wood
Type
H
S
H
S
H
S
H
S
H
S
H
S
H
S
H
S
H
Mill
Process
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Emission Point
Description
C102 subst. (low) seal
tank vent
C102 subst., (low) seal
tank vent
El-stage (0%) tower vent
El -stage (0%) tower vent
El-stage (0%) washer
vent
El-stage (0%) washer
vent
El-stage (0%) seal tank
vent
El-stage (0%) seal tank
vent
El-stage (100%) tower
vent
El-stage (100%) tower
vent
El -stage (100%) washer
vent
El -stage (100%) washer
vent
El-stage (100%) seal
tank vent
El-stage (100%) seal
tank vent
El -stage (high) tower
vent
El-stage (high) tower
vent
El-stage (high) washer
vent
Basis for
Emission Factor
Extrapolated from
EP Code 87
Extrapolated from
EP Code 88
Extrapolated from
EP Code 93
Extrapolated from
EP Code 94
Ratioed from EP
Code 94
Site 5 (P5 DG) ,
Site 2 (P7)
Extrapolated- from
EP Code 93
Extrapolated from
EP Code 94
Extrapolated from
EP Code 99
Extrapolated from
EP Code 100
Ratioed from EP
Code 100
Site 5 (SP5)
Extrapolated from
EP Code 99
Extrapolated from
EP Code 100
Extrapolated from
EP Code 105
Extrapolated from
EP Code 106
Site 4 (HP9, WW5)
                           B-25
-------
TABLE B-7 .  EMISSIONS SOURCES"AND DATA FACTORS  (CONTINUED)
EP
Code
106
107
108
109
110
111
112
113
114
115
116
117
118
119
120
121
122
Wood
Type
S
H
S
H
S
H
S
H
S
H
S
H
S
H
S
H
S
Mill
Process
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Emission Point
Description
El-stage (high) washer
vent
El-stage (high) seal
tank vent
El-stage (high) seal
tank vent
El-stage (low) tower
vent
El-stage (low) tower
vent
El-stage (low) washer
vent
El-stage (low) washer
vent
El-stage (low) seal tank
vent
El-stage (low) seal tank
vent
Dl-stage (0%) tower vent
Dl-stage (0%) tower vent
Dl-stage (0%) washer
vent
Dl-stage (0%) washer
vent
Dl-stage (0%) seal tank
vent
Dl-stage (0%) seal tank
vent
Dl-stage (100%) tower
vent
Dl-stage (100%) tower
vent
Basis for
Emission Factor
Site 4 (SV5,
SP6),
Site 1 (SP7)
Extrapolated from
EP Code 105
Extrapolated from
EP Code 106
Extrapolated from
EP Code 111
Extrapolated from
EP Code 112
Site 1 (HP3)
Site 1 (SP7)
Extrapolated from
EP Code 111
Extrapolated from
EP Code 112
Extrapolated from
EP Code 117
Site 5 (P6 DG)
Ratioed from EP
Code 118
Extrapolated from
EP Code 116
Extrapolated from
EP Code 117
Extrapolated from
EP Code 118
Extrapolated from
EP Code 123
Extrapolated from
EP Code 124
                            B-26
-------
TABLE B-7.  EMISSIONS SOURCES AND DATA FACTORS  (CONTINUED)
EP
Code
123
124
125
126
127
128
129
130
131
132
133
134
135
136
137
138
139
Wood
Type
H
S
H
S
H
S
H
S
H
S
H
S
H
S
H
S
H
Mill
Process
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Emission Point
Description
Dl-stage (100%) washer
vent
Dl-stage (100%) washer
vent
Dl-stage (100%) seal
tank vent
Dl-stage (100%) seal
tank vent
Dl-stage (high) tower
vent
Dl-stage (high) tower
vent
Dl-stage (high) washer
vent
Dl-stage (high) washer
vent
Dl-stage (high) seal
tank vent
Dl-stage (high) seal
tank vent
Dl-stage (low) tower
vent
Dl-stage (low) tower
vent
Dl-stage (low) washer
vent
Dl-stage (low) washer
vent
Dl-stage (low) seal tank
vent
Dl-stage (low) seal tank
vent
E2 -stage tower vent
Basis for
Emission Factor
Assumed the same
as EP Code 129
Assumed the same
as EP Code 130
Extrapolated from
EP Code 123
Extrapolated from
EP Code 124
Extrapolated from
EP Code 129
Extrapolated from
EP Code 130
Ratioed from EP
Code 130
Site 3 (SP8,
SP11)
Extrapolated from
EP Code 129
Extrapolated from
EP Code 130
Extrapolated from
EP Code 135
Extrapolated from
EP Code 136
Site 1 (HVIA)
Site 1 (SP8, SP9)
Site 2 (P9)
Extrapolated from
EP Code 135
Assumed the same
as EP Code 137
Extrapolated from
EP Code 141
                           B-27
-------
TABLE B-7.  EMISSIONS  SOURCES AND DATA FACTORS  (CONTINUED)
EP
Code
140
141
142
143
144
145
146
147
148
149
150
151
152
153
154
155
156
Wood
Type
S
H
S
H
S
H
S
H
S
H
S
H
S
H
S
H
H
Mill
Process
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Digesters
Digesters
Emission Point
Description
E2- stage tower vent
E2-stage washer vent
E2- stage washer vent
E2- stage seal tank vent
E2 -stage seal tank vent
D2- stage tower vent
D2- stage tower vent
D2- stage washer vent
D2- stage washer vent
D2- stage seal tank vent
D2- stage seal tank vent
H- stage (0.5-2%) washer
vent
H-stage (0.5-2%) washer
vent
H-stage (0.5-2%) seal
tank vent
H-stage (0.5-2%) seal
tank vent
batch relief gases
continuous relief gases
Basis- for
Emission Factor
Extrapolated from
EP Code 142
Ratioed from EP
Code 111
Ratioed from EP
Code 112
Extrapolated from
EP Code 141
Extrapolated from
EP Code 142
Extrapolated from
EP Code 147
Extrapolated from
EP Code 148
Assumed the same
as EP Code 135
Assumed the same
as EP Code 136
Extrapolated from
EP Code 147
Extrapolated from
EP Code 148
Ratioed from EP
Code 152
Site 5 (P7 DG) ,
Site 2 (P8)
Extrapolated from
EP Code 151
Extrapolated from
EP Code 152
Assumed the same
as EP Code 156
Site 4 (WW1)
                            B-28
-------
TABLE B-7.  EMISSIONS SOURCES AND DATA FACTORS  (CONTINUED)
EP
Code
157
158
159
160
161
162
163
164
165
166
167
168
169
170
171
172
173
Wood
Type
S
S
S.
S
S
S
H
S
H
S
H
S
H
S
H
S
H
Mill
Process
NCG System
NCG System
Tall Oil
Recovery
Tall Oil
Recovery
NCG System
NCG System
Digesters
Digesters
Digesters
Digesters
Digesters
Digesters
Digesters
Digesters
Digesters
Digesters
Digesters
Emission Point
Description
batch turpentine
condenser
cont . turpentine
condenser
batch vent
continuous vent
turpentine condensates
turpentine condensates
(IMP)
batch blow condensates
batch blow condensates
batch blow gases
batch blow gases
continuous blow gases I
continuous blow gases I
continuous blow gases ND
continuous blow gases ND
continuous blow
condensates I
continuous blow
condensates I
continuous blow
condensates ND
Basis for
Emission. Factor
Assumed the same
as EP Code 158
Site 3 (WW3)
Reference 8
Reference 8
Site 3 (WW3) ,
Site 1 (WW3)
Assumed the same
as EP Code 161
Site 1 (WW1, HP1)
Site 2 (WW4,
SP1),
Site 3 (WW2A)
Extrapolated from
EP Code 177
Site 3 (WW24,
SP1)
Site 4 (HP1)
Ratioed from EP
Code 167
Ratioed from EP
Code 170
Site 1 (SP2,
SP1),
Site 3 (WW2B) .
Assumed the same
as EP Code 173
Assumed the same
as .EP Code 174
Site 4 (WW1)
                           B-29
-------
TABLE B-7.  EMISSIONS SOURCES AND:DATA FACTORS'(CONTINUED)
EP
Code
174
175
176
177
178
181
182
183
184
185
186
187
188
189
190
191
192
Wood
Type
S
H
S
H
S
H
S
S
H
H
S
H
S
H
S
H
S
Mill
Process
Digesters
Knotters
Knotters
Washers
Washers
Washers
Washers
Washers
Washers
Evaporators
Evaporators
Evaporators
Evaporators
Evaporators
Evaporators
Oxygen
Delig.
Oxygen
Delig.
Emission Point
Description
continuous blow
condensates ND
hood vent
hood vent
hood, vent
hood vent
deckers /screens
deckers /screens
foam tank
foam tank
vent
vent
condensates
condensates
surface cond.
condensates
surface cond.
condensates
blow tank
blow tank
Basis for
Emission Factor
Site 3 (WW2b)
Extrapolated from
EP Code 177
Extrapolated from
EP Code 178
Site 4 (HV1, HP3,
HP6, HP4),
Site 1 (HP1)
Site 4 (SV1, SP1,
SP2, SP3, SP4)
Extrapolated from
EP Code 177
Extrapolated from
EP Code 178
Site 2 
-------
TABLE B-7.  EMISSIONS  SOURCES AND  DATA FACTORS (CONTINUED)
EP
Code
193
194
197
198
199
200
201
202
203
204
205
206
207
210
. 211
212
Wood
Type
H
S
H
S
H
S
H
S
H
S
S
H
S
H
S
H
Mill
Process
Oxygen
Delig.
Oxygen
Delig.


Sulfite
Digesters
Sulfite
Digesters
Sulfite
Digesters
Sulfite
Digesters
Sulfite
Evaporators
Sulfite
Evaporators
Sulfite NCG
System
Sulfite
Washer
Sulfite
Washer
Sulfite
Washer
Sulfite
Washer
Sulfite
Digesters
Emission Point
Description
washer tank vent
washer tank vent
weak black liquor
storage tank
weak black liquor
storage tank
batch relief gases
batch relief gases
batch blow gases
batch blow gases
multi effect evap. vent
multi effect evap. vent
turpentine condenser
hood vent
hood vent
decker vent
decker vent
blow condensates
Basis for
Emission Factor
Ratioed from EP
Code 194
Site 1 (SP4, SP5)
Site 4 (HP2,
HP4),
Site 1 (HP1)
Site 3 (SP3,
SP10) ,
Site 1 (SP2) ,
Site 4 (SP6)
Extrapolated from
EP Code 206
Extrapolated from
EP Code 207
Extrapolated from
EP Code 206
Extrapolated from
EP Code 207
Assumed the same
as EP Code 185
Assumed the same
as EP Code 186
Assumed the same
as EP Code 158
Ratioed from EP
Code 207
Site 5 (PI DG)
Extrapolated from
EP Code 206
Extrapolated from
EP Code 207
Ratioed from EP
Code 213
                            B-31
-------
TABLE B-7.  EMISSIONS  SOURCES  AND  DATA FACTORS (CONTINUED)
EP
Code
213
214
215
216
217
218
219
220
221
228
229
230
231
232
233
234
Wood
Type
S
H
S
H
S
H
S
H
S
H
S
H
S
H
S
S
Mill
Process
Sulfite.
Digesters
Sulfite
Washer
Sulfite
Washer
Sulfite
Sulfite
Sulfite
Oxygen
Delig.
Sulfite
Oxygen
Delig.
Sulfite
Oxygen
Delig.
Sulfite
Oxygen
Delig.
Sulfite
Washer
Sulfite
Washer
Sulfite
Washer
Sulfite
Washer
Washers
Washers
Bleaching
Emission Point
Description
blow condensates
waste liquor
waste liquor
weak black liquor
storage tank
weak black liquor
storage tank
blow tank
blow tank
washer tank vent
washer tank vent
foam tank vent
foam tank vent
improved washer vent I
improved washer vent I
improved washer vent I
improved washer vent I
scrubber effluent
Basis for
Emission Factor
Site 5 (PI DG)
Not used in Model
Plants
Not used in Model
Plants
Ratioed from EP
Code 217
Site 5 (P2 DG)
Extrapolated from
EP Code 220
Assumed the same
as EP Code 192
Ratioed from EP
Code 221
Site 5 (P4 DG)
Extrapolated from
EP Code 220
Extrapolated from
EP Code 221
Ratioed from EP
Code 231
Site 3 (SP2)
Ratioed from EP
Code 233
Site 1 (SP1, SP3)
Site 3 (WW1) ,
Site 1 (WW6)
                            B-32
-------
TABLE B-7.  EMISSIONS SOURCES AND DATA FACTORS  (CONTINUED)
EP
Code
235
236
237
301
302
303
304
305
306
307
308
309
310
311
312
313
Wood
Type
S
H
S
H
S
H
S
H
S
H
S
H
S
H
S
H
Mill
Process
Kraft
Kraft
Sulfite
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Emission Point
Description
covered weak black
liquor tank
covered weak black
liquor tank
covered weak black
liquor tank
E2-stage (low) tower
vent
E2-stage (low) tower
vent
E2-stage (low) washer
vent
E2- stage (low) washer
vent
E2- stage (low) seal tank
vent
E2 -stage (low) seal tank
vent
E2- stage (high) tower
vent
E2 -stage (high) tower
vent
E2- stage (high) washer
vent
E2- stage (high) washer
vent
E2 -stage (high) seal
tank vent
E2- stage (high) seal
tank vent
E2- stage (100%) tower
vent
Basis for
Emission Factor
Site 1 (SP2) ,
Site 4 (SP2) ,
Site 3 (SP3,
SP10)
Site 1 (HP1) ,
Site 4 (HP2)
Site 5 (P2 DG)
Reference 8
Reference 8
Reference 8
Reference 8
Reference 8
Reference 8
Reference 8
Reference 8
Reference 8
Reference 8
Reference 8
Reference 8
Reference 8
                           B-33
-------
          TABLE  B-7.   EMISSIONS SOURCES-AND DATA FACTORS  (CONTINUED)
EP
Code
314
315
316
'317
318
401
402
403
404
405
406
407
408
409
410
Wood
Type
S
H
S
H
S
H
S
H
S
H
S
H
S
H
S
Mill
Process
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Oxygen
Delig.
Oxygen
Delig.
Oxygen
Delig.
Oxygen
Delig.
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Bleaching
Emission Point
• Description
E2-stage (100%) tower
vent
E2- stage (100%) washer
vent
E2- stage (100%) washer
vent
E2-stage (100%) seal
tank vent
E2-stage (100%) seal
tank vent
blow tank
blow tank.
washer tank vent
washer tank vent
EOF- stage (100%) tower
vent
EOP- stage (100%) tower
vent
EOP- stage (100%) seal
tank vent
EOP-stage (100%) washer
vent
EOP-stage (100%) washer
vent
EOP-stage (100%) seal
tank vent
Basis for
Emission Factor
Reference 8
Reference 8
Reference 8'
Reference 8
Reference 8
Reference 9
Reference 9
Reference 9
Reference 9
Reference 9
Reference 9
Reference 9
Reference 9
Reference 9
Reference 9
DG'» Disolving  grade; H * Hardwood; S * Softwood
a Emission factors were extrapolated based on estimated relative emissions
  from each  unit  in a series of processing units.
b Emission factor were estimated based on the hardwood/softwood ratio.
                                         B-34
-------
estimate emissions for other situations where data were available for some
units in the series but not for all units.  This latter set of factors was
developed using analytical emission models developed under other EPA
programs.10   A complete discussion of the development of these ratios and
factors can be found in a separate document.n
     The Agency recognizes the shortcomings associated with emission factor
determinations by methods other than direct vent measurements.
Consequently, when vent measurement data were identified for an emission
point, those data were weighted heavily in the determination of an emission
factor for that emission point.  When no vent measurement data were found,
estimated values based on the procedures described above were used instead.
Additional measurement data are currently being collected for emission
points associated with pulp and paper manufacturing.  The list of emission
factors presented here will be updated in the future when warranted by new
data.
B.I2 EMISSION FACTORS
     This section presents a listing of emission factors developed for a
group of individual constituents at pulp and paper mills using procedures
described previously in this document, and as detailed in a separate
summary document.12 Separate emission factors are presented in Table B-8
for each emission source listed in Table B-7.
                                    B-35
-------
TABLE B-8. -EMISSION FACTORS-FOR'INDIVIDUAL 'SOURCES AND COMPOUNDS tg/Mg pulp)-
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl meroaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2, 4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet a 1 dehyde
P ropionaldehyde
DACETON-BF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobehzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
3
0 . 14272
28.73723
0.3
0.24772
0
0
0
0
0
0
210
105
0.32967
11.3
0
0
0
0
0
0
0
0
0
0
0
0.68891
0
0
0
0
0
0
0
0
0
0
0
0
0
41.60353
251.6035
41.41658
0
4
0.03659
2.07739
0
0.10322
0
0
0
0
0
0
210
0
0.35834
10
0
0
0
0
0.1
0
0
0
0
0
0
0.00177
0.01731
0.00812
0.03718
0.6
0
0.5
0
0
0.03071
0
0
0
0
13.79686
223.7969
13.41229
0
7 8
70
50
0
25
0
0
0
0
0
0
0
0
3
5.28889
0
0
0
0
0
0.3
1.75
0
10
0
0
2
6
16
0
0
0
0
0
0
12
0
0
0
0
119.5889
119.5889
198.3389
0
70
50
0
25
0
0
0
0
0
0
0
0
3
5.03313
0
0
0
0
0
0.3
1.7
0
10
0
0
2
6
16
0
0
0
0
0
0
12
0
0
0
0
119.3331
119.3331
198.0331
0
19
0.01317
6.30142
0
0.0258
0
0
0
0
0
0.1048
10
1.95
5.01671
40
0
0
0
0
0
0
0
0
0
0
0
0.02385
0.02077
0.08122
0.00372
0.25
0
0
2
0
0.07677
0
0
0
6.74112
51.79654
61.90134
55.53784
0
20
1
0.49
0
1.4
0
0
0
0
0.02
0
10
0
20
50
.0
0
0
0
0
0
0
0
0
0
0
0.02
0.13
0.38
0.01
2..1
0
0
0
0
3
0
0
0
60
77.52
87.52
118.55
0
                                     B-36
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, l-Trichloroetan«
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltriaulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
39
70
50
0
25
0
0
0
0
0
0
0
0
3
5.28889
0
0
0
0
0
0.37
1.75
0
10
0
0
2
6
16
0
0
0
0
0
0
12
0
0
0
0
119.6589
119.6589
198.. 4089
0
40 41 42 45 46
70
50
0
25
0
0
0
0
0
0
0
0
3
5.03313
0
0
0
0
0
0.37
1.75
0
10
0
0
2
6
16
0
0
0
0
0
0
12
0
0
0
0
119.4031
119.4031
198.1531
0
67
100
0
20
0
0
0
0
0
0
0
0
3
1.41742
0
0
0
0
0
0
0
0
0
0
0
1
1.4
1.2
0
0.002
0
0
0
0
9
0
0
0
0
137.0194
137.0194
201.0194
0
67
100
0
20
0
0
0
0
0
0
0
0
3
2.29962
0
0
0
0
0
0
0
0
0
0
0
1
1-4 .
1.2
0
0.002
0
0
0
0
9
0
0
0
0
137.9016
137.9016
201.9016
0
0 . 14272
28.73723
0.3
0.24772
0
0
0
0
0
0
210
105
0.32967
5.27414
0
0
0
0
0
0
0
0
0
0
0
0.68891
0
0
0
0
0
0
0
0
0
0
0
0
0
35.57767
245.5777
35.39072
0
0.03659
2.07739
0
0.10322
0
0 I
0
0
0
0
210
0
0.35834
6.20716
0
0
0
0
0.1
o •
0
0
0
0
0
0.00177
0.01731
0.00812
0.03718
0.6
0
0.5
0
0
0.03071
0
0
0
0
10.00402
220.004
9.61945
0
                          B-37
-------
TABLE B-8.  EMISSION FACTORS FOR-INDIVIDUAL SOURCES AND •
            COMPOUNDS  (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl aulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
P ropionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
47 48 49 50 53 54
2.7
500
0
2
0
0
0
0
0
0
• o
0
6
0.89839
0
0
0
0
0
0.37
1.75
0
1
0
0
0.2
0.7
- 1.1
0
0.00003
0
0.0025
0
0
9
0
0
0
0
520.2709
520.2709
519.7209
0
2 . 7
500
0
2
0
0
0
0
0
0
0
0
6
0.80657
0
0
0
0
0
0.37
1.75
0
1
0
0
0.2
0.7
1.1
0
0.00003
0
0.0025
0
0
9
0
0
0
0
520.1791
520.1791
519.6291
0
3.5
300
0
0.7
0
0
0
0 •
0
0
0
0
3.3
0.24077
0
0
0
0
0
0
0
0
0
0
0
0.16
3
0.6
0 '
0.00006
0
0
. 0
0
6
0
0
0
0
314.0008
314.0-008
314.2008
0
3 . 5
300
0
0.7
0
0
0
0
0
0
0
0
3.3
0.36852 .
0
0
0
0
0
0
0
0
0
0
0
0.16
3
0.6
0
0.00006
0
0
0
0
6
0
0
0
0
314.1286
314.1286
314.3286
0
0.07319
7.6171
0.29
0.72253
0
0
0
0
0
0.01344
50
105
0.50167
0.85725
0
0
0
0
0.3
•}
0
0
0
0
0
0.04416
0.11249
0
0.07436
0.06
0
1.8
8
0.3
0.29942
0
0
0
0
12.90462
62.91806
20.2505
0
0.0022
0.62322
0.3
0.00103
0
0
0
0
0
0.02015
50
125
0.14333
1.93089
0
0
0
0
0
0
0
0
0
0
0
0.00128
0
0.00002
0
0.06
0
0.5
0
0.3
0
0
0
0
0
3.85977
53.87992
3.71864
0
                           B-38
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Fur an
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acetaldehyde
P ropionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltriaulfide
Carbon diaulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
55
2 . 7
500
0
2
0
0
0
0
0
0
0
0
6
2.21554
. 0
0
0
0
0
3.7
1.75
0
8
0
0
0.2
0.7
1.1
0
0.00003
0
0.0025
0
0
9
0
0
0
0
524.9181
524.9181
531.3681
0
56 57 58
2.7
500
0
2
0
0
0
0
0
0
0
0
6
1.96125
0
0
0
0
0
0.37
1.75
0
8
0
0
0.2
0.7
1.1
0
0.00003
0
0.0025
0
0
9
0
0
0
0
521.3338
521.3338
527.7838
• o
3.5
300
0
0.7
0
0
0
0
0
0
0
0
3.3
0.59376
0
0
0
0
0
0
0
0
0
0
0
0.16
3
0.6
0
0.00006
0
0
0
0
6
0
0
0
0
314.3538
314.3538
314.5538
0
3 .5
300
0
0.7
0
0
0
0
0
0
0
0
3.3
0.89609
0
0
0
0
0
0
0
0
0
0
0
0.16
3
0.6
0
0.00006
0
0
0
0
6
0
0
0
0
314.6562
314.6562
314.8562
0
61
0 .07319
7.6171
0.29
D. 72253
0
0
0
0
0
0.01344
50
105
0.50167
1.16536
0
0
0
0
0.3
0
0
0
0
0
0
0.04416
0.11249
0
0.07436
0.06
0
1.8
8
0.3
0.29942
0
0
0
0
13.21273
63.22617
20.55861
0
62
0.0022
0.62322
0.3
0.00103
0
0
0
0
0
0.02015
50
125
0.14333
1.93089
0
0
0
0
0
0
0
0
0
0
0
0.00128
0
0 .00002
0
0.06
0
0.5
0
0.3
0
0
0
0
0
3.85977
53.87992
3.71864
0
                          B-39
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS  (g/Mg pulp)  (CONTINUED)
Compound Names

Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl gulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha terpinol
Acrolein
Acet aldehyde
P ropionaldehyde
DACETON-EF
'Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
63

460
0

0
0
0
0
0
0
0
0
3
4.09718
0
0
0
0
0
0.37
1.75
0
10
0
0
2.5
1.2
0.5
0
0
0
0
0
0
8.1
0
0
0
0
486.7672
486.7672
497.7172
0
64

200
0
3
0
0
0
0
0
0
0
0
3
3.79904
0
0
0
0
0.0002
0.37
1.75
0
10
0
0
0.05
0.2
0.3
0.06
0.003
0
0.03
0
0
1
0
0
0
0
211.7522
211.7522
221.562
0
65
2
100
0
10
0
0
0
0
0
0
0
0
0.03
1.09805
0
0
0
0
0
0
0
0
0
0
0
0.14
2.3
0.08
0
0
0
0
0
0
15
0
0
0
0
128.6481
128.6481
130.6181
0
66

30
0
2
0
0
0
0
0
0
0
0
3
1.73577
0.
0
0
0
0.002
0
0
0
0
0
0
0.1
1
0.8
0
0.001
0
0
0
o •
3.4
0
0
0
0
42.03877
42.03877
40.03677
0
69

28.73723
0.3
0.24772
0
0
0
0
0
0
210
105
0.32967
5.27414
0
0
0
0
0
0
-o
0
0
0
0
0.68891
0
0
0
0
0
0
0
0
0
0
0
0
0
35.57767
245.5777
35.39072
0
70
0.03659
2.07739
0
0.10322
0
0
0
0
0
0
210
0
0.35834
4.31903
0'
0
0
0
0.1
0
0'
0
0
0
0
0.00177
0.01731
0.00812
0.03718
0.6
0
0.5
0
0
0.03071
0
0
0
0
8.11589
218.1159
7.73132
0
                           B-40
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl di sulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2f 4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
P ropionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon disulfide
Total HC
Other
Total . HAP
Total VOC
TRS
EP Codes
71
1 . 95
415
0.3
2.4
0
0
0
0
0
0
210
105
0.46
11.3
0
0
0
0
0
0
0
0
0
0
0
7.8
0
0
0
0
0 '
0
0
0
0
0
0
0
0
437.26
647.26
438.75
0
72 73
0 . 5
30
0
1
0
0
0
0
0
0
210
0
0.5
10
0
0
0
0
0.1
0
0
0
0
0
0
0.02
0.2
0.1
0.2
0.6
0
0.5
0
0
0.4
0
0
0 •
0
43.42
253.42
43.52
0
1 . 40091
311.2622
0.00266
1.30507
0
0
• 0
0
0
0
5.32471
2.66236
0.04193
0.72566
0
0
0
0
0
0
0
0
0
0
0
4.82303
0
0
0
0
0
0
0
0
0
0
0
0
0
318.1605
323.4852
319.5195
0
74
0 . 35921
22.50088
0
0.54378
0
0
0
0
0
0
5.324
0
0.04558
0.64217
0
0
0
0
0.00139
0
0
0
0
0
0
0.01237
0.12574
0.06616
0.06515
0.01923
0
0.02273
0
0
0.27675
0
0
0
0
24.25678
29.58078
24.63417
0
/5 76
1 . 95
415
0.3
2.4
0
0
0
0
0
0
210
105
0.46
5.27414
0
0
0
0
0
0
0
0
0
0
0
7.8
0
0
0
0
0
0
0
0
0
0
0
0
0
431.2341
641.2341
432.7241
0
0.5
30
0
1
0
0
0
0
0
0
210
0
0.5
6.20716
0
0
0
0
0.1
0
0
0
0
0
0
0.02
0.2
0.1
0.2
0.6
0
0.5
0
0
0.4
0
0
0
0
3-9.62716
249.6272
39.72716
0
                          B-41
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS  (g/Mg pulp)  (CONTINUED)
Compound NameS
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Fur an
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acetaldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltriaulfide
Carbon diaulfide
Total HC
Other
Total HAP
Total, VOC
TRS
EP Codes
77
0 .35921
311.2622
0
0.54378
0
0
0
0
0
0
5.324
0
0.04133
0.39861
0
0
0
0
0.00139
0
0
0
0
0
0
4.82303
0.12574
0.06616
0.06515
0.01923
0
0.02273
0
0
0.27675
0
0
0
0
317.5809
322.9049
3179626
0
78 79
1.40091
22.50088
0.00266
1.30507
0
0
0
• o
0
0
5.32471
2.66236
0.04558
0.33869
0
0
0
0
0
0
0
0
0
0
0
0.01237
0
0
0
0
0
0
0
0
0
0
0
0 •
0
24.20525
29.52996
25.56058
0
1
110
0.29
7
• o
0
0
0
0
0.2
50
105
0.7
0.85725
0
0
0
0
0.3
0
0
0
0
0
0
0.5
1.3
0
0.4
0.06
0
1.8
8
0.3
3.9
0
0
0
0
127.0073
177.2073
135.4073
0
80 81
0.03
9
0.3
0.01
0
0
0
0
0
0.3
50
125
0.2
1.93089
0
0
0
0
0
0
0
0
0
0
0
0.00128
. 0
0.0003
0
0.06
0
0.5
0
0.3
0
0
0
0
0
12.30247
62.60247
12.13247
0
0. 71842
82.50323
0.0-0257
3.80647
0
0
0
0
0
0.15355
1.268
2.66236
0.06381
0.05505
0
0
0
0
0.00417
0
0
0
0
0
0
0.30917
0.81734
0
0.1303
0.00192
0
0.08181
0.06678
0.01223
2.69835
0
0
0
0
90.35612
91'. 77767
91.20364
0
82
0.02155
6.75026
0.00266
0.00544
0
0
0
0
0
0.23033
1.26779
3.16947
0.01823
0.124
0
0
0
0
0
0
0
0
0
0
0
0.00128
0
0.0002
0
0.00192
0
0.02273
0
0.01223
0
0
0
0
0
6.93895
8.43707
6.94227
0
                           B-42
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride •
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
Propionaldehyde
DACETOW-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
D imet hy It ri sulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
83
1
110
0.29
7
0
0
0
0
o.
0.2
50
105
0.7
1.16536
0
0
0
0
0.3
0
0
0
0
0
0
0.5
1.3
0
0.4
0.06
0
1.8
8
0.3
3.9
0
0
0
0
127.3154
177.5154
135.7154
0
84 85
0.03
9
0.3
0.01
0
0
0
0
0
0.3
50
125
0.2
1.93089
0
0
0
0
0
0
0
0
0
0
0
0.00128
0
0.0003
0
0.06
0
0.5
0
0.3
0
0
0
0
0
12.30247
62.60247
12.13247
0
0.71842
82.50323
0.00257
3.80647
0
0
0
0
0
0.15355
1.268
2.66236
0.06381
0.07484
0
0
0
0
0.00417
0
0
0
0
0
0
0.30917
0.81734
0
0.1303
0.00192
0
0.08181
0.06678
0.01223
2.69835
0
0
0
0
90.37591
91.79746
91.22343
0
86
0 . 02155
6.75026
0.00266
0.00544
0
0
0
0
0
0.23033
1.26779
3.16947
0.01823
0.124
0
0
0
0
0
0
0
0
0
0
0
0.00128
. 0
0.0002
0
0.00192
0
0.02273
0
0.01223
0
0
0
0
0
6.93895
8.43707
6.94227
0
87
1. 95
415
0.3
2.4
0
0
0
0
0
0
210
105
0.46
5.27414
0
0
0
0
0
0
0
0
0
0
0
7.8
0
0
0
0
0
0
0
0
0
0
0
0
0
431.2341
641.2341
432.7241
0
88
0.5
30
o
1
0
0
0
0
0
0
210
0
0.5
4.31903
0
0
0
0
0.1
0
0
0
0
0
0
0.02
0.2
0.1
0.2
0.6
0
0.5
0
0
0.4
0
0
0
0
37.73903
247.739
37. .83903
0
                          B-43
-------
TABLE B-8.  EMISSION FACTORS FOR-INDIVIDUAL SOURCES AND
            COMPOUNDS  (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl Jcetone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl diaulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chloropheno 1
Beta Pinene
Alpha Terpinol
Acrolein
Acetaldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon diaulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
89

311.2622
0.00266
1.30507
0
0
0
0
0
0
5.32471
2.66236
0.04193
0.34738
0
0
0
0
0
0
0
0
0
0
0
4.82303
0
0
0
0
0
0
0
0
0
0
0
0
0
317.7823
323.107
319.1412
0
90
0.35921
22.50088
0
0.54378
0
0
0
0
0
0
5.324
0
0.04558
0.27736
0
0
0
0
0.00139
0
0
0
0
0
0
0.01237
0.12574
0.06616
0.06515
0.01923
0
0.02273
0
0
0.27675
0
0
0
0
23.89197
29.21597
24.26936
0
91
2.19563
0.48472
0
3.09655
0
0
0
0
0.13
0.02687
3
3
3.58337
7.93455
0
0
0
0
0.3
0
0
0
0
0.01885
0
0.17664
0
0.08122
0
5
0
0
1
0
0.00384
0
0
0
1.54968
20.66089
23.68776
21,67168
0
92
2.19563
0.48472
0
3.09655
0
0
0
0
0.13
0.02687
3
3
3.58337
10.55217
0
0
0
0
0.3
0
0
0
0
0.01885
0
0.17664
0
0.08122
0
5
0
0
1
0
0.00384
0
0
0
1.54968
23.27851
26.30538
24.2893
0
93
30
7
0
30
0
0
0
0
0.13
0.4
3
3
5
7.93455
0
0
. 0
0
0.3
0
0
0
0
0.02
0
2
0
1
0
5
0
0
1
0
0.05
0
0
0
4
58.28455
61.68455
88.13455
0
94
30
7
0
30
- o
0
0
0
0.13
0.4
3
3
5
10.55217
0
0
0
0
0.3
0
0
0
0
0.02
0
2
0
1
0
5
0
0
1
0
0.05
0
0
0
4
60.90217
64.30217
90.75217
0
                           B-44
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2, 4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
P ropionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
D imethy It ri sulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
95
21.55246
5.25021
0
16.31342
0
0
0
0
0.00687
0.3071
0.07607
0.07607
0.45576
0.50954
0
0
0
0
0.00417
0
0
0
0
0.0014
0
1.23667
0
0.66156
0
0.16025
0
0
0.00835
0
0.03459
0
0
0
0.65903
24.62617
25.00934
46.39435
0
96
21.55246
5.25021
0
16.31342
0
0
0
0
0.00687
0.3071
0.07607
0.07607
0.45576
0.67763
0
0
0
0
0.00417
0
0
0
0
0.0014
0
1.23667
0
0.66156
0
0.16025
0
0
0.00835
0
0.03459
0
0
0
0.65903
24.79426
25.17743
46.56244
0
97
6.22096
5.40121
0
6.50274
0
0
0
0
0
0
0
0
4.58671
3.95654
0
0
0
0
0
0
0
0
0
0
0
0.18548
0.18171
0.09747
0
6
0
0
1
'0
0.4069
0
0
0
0
27.31876
27-.31876
29.95301
0
98
6.22096
5.40121
0
6.50274
0
0
0
0
0
0
0
0
4.58671
2.89633
0
0
0
0
0
0
0
0
0
0
0
0.18548
0.18171
0.09747
0
6
0
0
1
0
0.4069
0
0
0
0
26.25855
26.25855
28.8928
0
99
85
78
0
63
0
0
0
0
0
0
0
0
6.4
3.95654
0
0
0
0
0
0
0
0
0
0
0
2.1
2.1
1.2
0
6
0
0
1
0
5.3
0
0
0
0
168.0565
168.0565
247.6565
0
100
85
78
0
63
0
0
0
0
0
0
0
0
6.4
2.89633
0
0
0
0
0
0
0
0
0
0
0
2.1
2.1
1.2
0
6
0
0
1
0
5.3
0
0
0
0
166.9963
166.9963
246.5963
0
                          B-45
-------
TABLE B-8.  EMISSION FACTORS FOR-INDIVIDUAL SOURCES AND
            COMPOUNDS  (g/Mg pulp)  (CONTINUED)
Compound Names

Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl diaulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Fur an
1, 1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
P ropionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon diaulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
101

58.50229
0
34.25819
0
0
0
0
0
0
0
0
0.58337
0.25408
0
0
0
0
0
0
0
0
0
0
0
1.29851
1.32032
0.79388
0
0.1923
0
0
0.00835
0
3.66699
0
0
0
0
100.8699
100.8699
161.3602
0
102

58.50229
0
34.25819
0
0
0
0
0
0
0
0
0.58337
0.18599
0
0
0
0
0
0
0
0
0
0
0
1.29851
1.32032
0.79388
0
0.1923
0
0
0.00835
0
3i66699
0
0
0
0
100.8018
100.8018
161.2921
0
103
6.22096
5.40121
0
6.50274
0
0
0
0
0
0
0
0
4.58671
3.95654
0
0
0
0
0
0
0
0
0
0
0
0.18548
0.18171
0.09747
0
6
0
0
1
0
0.4069
0
0
0
0
27.31876
27.31876
29.95301
0
104

5.40121
0
6.50274
0
0
0
0
0
0
0
0
4.58671
2.89633
0
0
0
0
0
0
0
0
0
0
0
0.18548
0.18171
0.09747
0
6
0
0
1
0
0.4069
0
0
0
0
26.25855
26.25855
28.8928
0
105

78
0
63
0
0
0
0
0
0
0
0
6.4
3.95654
0
0
0
0
0
0
0
0
0
0
0
2.1
2.1
1.2
0
6
0
0
1
0
5.3
0
0
0
0
168.0565
168.0565
247.6565
0
106
85
78
0
63
o •
0
0
0
0
0
0
0
6.4
2.89633
0
0
0
0
0
0
0
0
0
0
0
2.1
2.1
1.2
0
6
0
0
1
0
5.3
0
0
0
0
166.9963
166.9963
246.5963
0
                           B-46
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS  (g/Mg pulp) (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl Jcetone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acetaldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
107
61.06531
58.50229
0
34.25819
0
0
0
0
0
0
0
0
0.58337
0.25408
0
0
0
0
0
0
0
0
0
0
0
1.29851
1.32032
0.79388
0
0.1923
0
0
0.00835
0
3.66699
0
0
0
0
100.8699
100.8699
161.3602
0
108 109
61.06531
58.50229
0
34.25819
0
0
.0
0
0
0
0
0
0.58337
0.18599
0
0
0
0
0
0
0
0
0
0
0
1.29851
1.32032
0.79388
0
0.1923
0
0
0.00835
0
3.66699
0
0
0
0
100.8018
100.8018
161.2921
0
2.19563
0.48472
0
3.09655
0
0
0
0
0.13
0.02687
3
3
3.58337
7.93455
0
0
0
0
0.3
0
0
0
0
0.01885
0
0.17664
0
0.08122
0
5
0
0
1
0
0.00384
0
0
0
1.54968
20.66089
23.68776
21.67168
0
110
2.19563
0.48472
0
3.09655
0
0
0
0
'0.13
0.02687
3
3
3.58337
10.55217
0
0
0
0
0.3
0
0
0
0
0.01885
0
0.17664
0
0.08122
0
5
0
0
1
0
0.00384
0
0
0
1.54968
23.27851
26.30538
24.2893
0
111
30
7
0
30
0
0
0
0
0.13
0.4
3
3
5
7.93455
0
0
0
0
0.3
0
0
0
0
0.02
0
2
0
1
0
5
0
0
1
0
0.05
0
0
0
4
58.28455
61.68455
88.13455
0
112
30
7
0
30
0
0
0
0
0.13
0.4
3
3
5
10.55217
0
0
0
0
0.3
0
0
0
0
0.02
0
2
0
1
0
5
0
0
1
0
0.05
0
0
0
4
60.90217
64.30217
90.75217
0
                          B-47
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL.SOURCES'AND
            COMPOUNDS (g/Mg pulp)  (CONTINUED)
Compound Names

Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl aulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2, 4,5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
P ropionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane.
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon diaulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
113

5.25021
0
16.31342
0
0
0
0
0.00687
0.3071
0.07607
0.07607
0.45576
0.50954
0
0
0
0
0.00417
0
0
0
0
0.0014
0
1.23667
0
0-. 66156
0
0.16025
0
0
0.00835
0
0.03459
0
0
0
0.65903
24.62617
25.00934
46.39435
0
114

5.25021
0
16.31342
0
0
0
0
0.00687
0.3071
0.07607
0.07607
0.45576
0.67763
0
0
0
0
0.00417
0
0
0
0
0.0014
0
1.23667
0
0.66156
0
0.16025
0
0
0.00835
0
0.03459
0
0
0
0.65903
24.79426
25.17743
46.56244
0
115

0.20774
0
0.30965
0
0
0
0
0
0
10
40
4.30004
15.79747
0
0
0
0
0
0
0
0
0
0
0
0.04416
0.03461
0.16245
0
0
0
0
0
0
0.92128
0
0
0
0
21.7774
31.7774
17.55055
0
116

0.20774
0
0.30965
0
0
0
0
0
0
10
40
4.30004
20.4.8362
0
0
0
0
0
0
0
0
0
0
0
0.04416
0.03461
0.16245
0
0
0
0
0
0
0.92128
0
0
0
0
26.46355
36.46355
22.2367
0
117

3
0
3
0
0
0
0
0
0
10
40
6
15.79747
0
0
0
0
0
0
0
0
0
0
0
0.5
0.4
2
0
0
0
0
0
0
12
0
0
0
0
42.69747
52.69747
37.69747
0
118
1
3
0
3
0
0
0
0
0
0
10
40
6
20.48362
0
0
0
0
0
0
0
0
0
0
0
0.5
0.4
2
0
0
0
0
0
0
12
0
0
0
0
47.38362
57.38362
42.38362
0
                           B-48
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acetaldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
119 120 121 122 123
0 . 71842
2.25009
0 .
1.63134
0
0
0
0
0
0
0.25356
1.01423
0.54691
0.9891
0
0
0
0
0
0
0
0
0
0
0
0.30917
0.25149
1.32313
0
0
0
0
0
0
8.30261
0
0
0
0
15.60384
15.8574
15.77535
0
0.71842
2.25009
0
1.63134
0
0
0
0
0
0
0.25356
1.01423
0.54691
1.3154
0
0
0
0
0
0
0
0
0
0
0
0.30917
0.25149
1.32313
0
0
0
0
0
0
8.30261
0
0
0
0
15.93014
16.1837
16.10165
• 0
0.00029
0.00069
0
0.00021
0
0
0
0
0
0
10
40
1.07501
0.04616
0
0
0
0
0
0
0
0
0
0
0
0.00018
0.00043
0.00049
0
0
0
0
0
0
0.00461
0
0
0
0
1.12778
11.12778
0.05306
0
0.00029
0.00069
0
0.00021
0
0
0
0
0
0
10
40
1.07501
0.03379
0
0
0
0
L °
L °
0
0
0
0
0
0.00018
0.00043
0.00049
0
0
0
0
0
0
0.00461
0
0
0
0
1.11541
11.11541
0.04069
0
0. 004
0.01
0
0.002
0
0
0
0
0
0
10
40
1.5
0.04616
0
0
0
0
0
0
0
0
0
0
0
0.002
0.005
0.006
0
0
0
0
0
0
0.06
0
0
0
0
1.63116
11.63ir6
0.13516
0
124
0 .004
0.01
0
0.002
0
0
0
0
0
0
10
40
1.5
0.03379
0
0
0
0
0
0
0
0
0
0
0
0.002
0.005
0.006
0
0
0
0
0
0
0.06
0
0
0
0.
1.61879
11.61879
0.12279
0
                          B-49
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AMD-
            COMPOUNDS (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl aulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
P ropionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
125 126 127 128 129 130
0 . 00287
0.0075
0
0.00109
0
0
0
0
0
0
0.25356
1.01423
0.13673
0.00296
0
0
0
0
0
0
0
0
0
0
0
0.00124
0.00314
0.00397
0
0
0
0
0
0
O.P4151
0
0
0
0
0.19814
0.4517
0.06428
0
0.00287
0.0075
0
0.00109
0
0
0
0
0
0
0.25356
1.01423
0.13673
0.00296
0
0
0
0
0
0
0
0
0
0
0
0.00124
0.00314
0.00397
0
0
0
0
0
0
0.04151
0
0
0
0
0.19814
0.4517
0.06428
0
0.00029
0.00069
0
0.00021
0
0
0
0
0
0
10
40
1.07501
0.06275
0
0
0
0
0
0
0
0
0
0
0
0.00018
0.00043
0.00049
0
0
0
0
0
0
0.00461
0
0
0
0
1.14437
11.14437
0.06965
0
0.00029
0.00069
0
0.00021
0
0
0
0
0
0
10
40
1.07501
0.10605
0
0
0
0
0
0
0
0
0
0
0
0.00018
0.00043
0.00049
0
0
0
0
0
0
0.00461
0
0
0
0
1.18767
11.18767
0.11295
0
0 . 004
0.01
0
0.002
0
0
0
0
0
0
10
40
1.5
0.06275
0
0
0 '
0
0
0
0
0
0
0
0
0.002
0.005
0.006
0
0
0
0
0
• 0
0.06
0
0
0
0
1.64775
11.64775
0.15175
0
0.004
0.01
0
0.002
0
0
0
0
0
0
10
40
1.5
0.10605
0
0
0
0
0
0
0
0
0
0
0
0.002
0.005
0.006
0
0
0
0
0
0
0.06
0
0
0
0
1.69105
11.69105
0.19505
0
                           B-50
-------
TABLE B-8.
EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
COMPOUNDS (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Fur an
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
P ropionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltri sulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
131
0 . 00287
0.0075
0
0.00109
0
0
0
0
0
0
0.25356
1.01423
0.13673
0.00403
0
0
0
0
0
0
0
0
0
0
0
0.00124
0.00314
0.00397
0
0
0
0
0
0
6.04151
0
0
0
0
0.19921
0.45277
0.06535
0
132 133
0 .00287
0.0075
0
0.00109
0
0
0
0
0
0
0.25356
1.01423
0.13673
0.00681
0
0
0
0
0
0
0
0
0
0
0
0.00124
0.00314
0.00397
0
0
0
0
0
0
0.04151
0
0
o-
0
0.20199
0.45555
0.06813
0
0.07319
0.20774
0
0.30965
0
0
0
0
0
0
10
40
4.30004
15.79747
0
0
0
0
0
0
0
0
0
0
0
0.04416
0.03461
0.16245
0
0
0
0
0
0
0.92128
0
0
0
0
21.7774
31.7774
17.55055'
0
134 135 136
0 .07319
0.20774
0
0.30965
0
0
0
0
0
0
10
40
4.30004
14.2528
0
0
0
0
0
0
0
0
0
0
0
0.04416
0.03461
0.16245
0
0
0
0
0
0
0.92128
0
0
0
0
20.23273
30.23273
16.00588
0
1
3
0
3
0
0
0
0
0
0
10
40
6
15.79747
0
0
0
0
0
0
0
0
0
0
0
0.5
0.4
2
0
0
0
0
0
0
12
0
0
0
0
42.69747
52.69747
37.69747
0
1
3
0
3 -
0
0
0
0
0
0
10
40
6
14.2528
0
0
0
0
0
0
0
0
0
0
0
0.5
0.4
2
0
0
0
0
0
0 .
12
0
0
0
0
41.1528
51.1528
36.1528
0
                          B-51
-------
TABLE B-8.   EMISSION FACTORS FOR--INDIVIDUAL SOURCES AND
             COMPOUNDS (g/Mg pulp)  (CONTINUED)

Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenrene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
137 138 139 140 141 142
0 . 71842
2.25009
0
1.63134-
0
0
0
0
0
0
0.25356
1.01423
0.54691
1.01447
0
0
0
0
0
0
0
0
0
0
0
0.30917
0.25149
1.32313
0
0
0
0
0
0
8.30261
0
0
0
0
15.62921
15.88277
15.80072
0
0.71842
2.25009
0
1.63134
0
0
0
0
0
0
0.25356
1.01423
0.54691
0.91528
0
0
0
0
0
0
0
0
0
0
0
0.30917
0.25149
1.32313
0
0
0
0
0
0
8.30261
0
0
0 .
0
15.53002
15.78358
15.70153
0
1.09782
0.24236
0
1.54827
0
0
0
0
0.065
0.01344
0
1.5
1.79168
3.96728
0
0
0
0
0.15
0
0
0
0
0.00942
0
0.08832
0
0.04061
0
2.5
0
0
0.5
0
0.00192
0
0
0
0.77484
10.33044
10.34388
10.83584
0
1.09782
0.24236
0
1.54827
0
0
0
0
0.065
0.01344
0
1.5
1.79168
5.27608
0
0
0
0
0.15
0
0
0
0
0.00942
0
0.08832
0
0.04061
0
2.5
0
0
0.5
0
0.00192
0
0
0
0.77484
11.63924
11.65268
12.14464
0
15
3.5
0
15
0
0
0
0
0.065
0.2
0
1.5
2.5
3.96728
0
0
0
0
0.15
0
0
0
0
0.01
0
1
0
0.5
0
2.5
0
0
0.5
0
0.025
0
0
0
2
29.14228
29.34228
44.06728
0
15
3.5
0
15
0
0
0
0
0.065
0.2
0
1.5
2.5
5.27608
0
0
0
0
0.15
0
0
0
0
0.01
0
1
0
0.5
0
2.5
0
0
0.5
0
0.025
0
0
0
2
30.45108
30.65108
45.37608
0
                            B-52
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl diaulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2, 4, 5-Trichlof ophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon di sulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
143
10 . 77623
2.6251
0
8.15671
0
0
0
0
0.00343
0.15355
0
0.03803
0.22788
0.25477
0
0
0
0
0.00209
0
0
0
0
0.0007
0
0.61834
0
0.33078
0
0.08012
0
0
0.00417
0
0.0173
0
0
0
0.32951
12.31309
12.46664
23.19716
. 0
144 145
10.77623
2.6251
0
8.15671
0
0
0
0
0.00343
0.15355
0
0.03803
0.22788
0.33882
0
0
0
0
0.00209
0
0
0
0
0.0007
0
0.61834
0
0.33078
0
0.08012
0
0
0.00417
0
0.0173
0
0
0
0.32951
12.39714
12.55069
23.28121
0
0 .00029
0.00069
0
0.00.021
0
0
0
0
0
0
10
40
1.07501
0.04616
0
0
0
0
0
0
0
0
0
0
0
0.00018
0.00043
0.00049
0
0
0
0
0
0
0.00461
0
0
0
0
1.12778
11.12778
0.05306
0
146
0 . 00029
0.00069
0
0.00021
0
0
0
0
0
0
10
40
1.07501
0.03379
0
0
0
0
0
0
0
0
0
0
0
0.00018
0.00043
0.00049
0
0
0
0
0
0
0.00461
0
0
0
0
1.11541
11.11541
0.04069
0

147
0 . 004
0.01
0
0.002
0
0
0
0
0
0
10
40
1.5
0.04616
0
0
0
0
0
0
0
0
0
0
0
0.002
0.005
0.006
0
0
0
0
0
0
0.06
0
0
0
0
1.63116
11.63116
0.13516
0

148
0.004
0.01
0
0.002
0
0
0
0
0
0
10 '
40
1.5
0.03379
0
0
0
0
0
0
0
0
0
0
0
0.002
0.005
0.006
0
0
0
0
0
0
0.06
0
0
0
0
1.61879
11.61879
0.12279
0
                          B-53
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL'SOURCES"AND
            COMPOUNDS  (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl aulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2, 4,5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophcnol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon diaulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
149 150 151 152 153 154
0 . 00287
0.0075
0
0.00109
0
0
0
0
0
0
0.25356
1.01423
0.13673
0.00296
0
0
0
0
0
0
0.
0
0
0
0
0.00124
0.00314
0.00397
0
0
0
0
0
0
0.04151
0
0
0
0
0.19814
0.4517
0.06428
0
0.00287
0.0075
0
0.00109
0
0
0
0
0
0
0.25356
1.01423
0.13673
0.00296
0
0
0
0
0
0
0
0
0
0
0
0.00124
0.00314
0.00397
0
0
0
0
0
0
0.04151
0
0
0
0
0.19814
0.4517
0.06428
0
0.18
91
0
0.25
0
0
0
0
0
1.56
10
1.95
7
40
0
0
0
0
0
0
0
0
0
0
0
0.27
0.24
1
0.02
0.25
0
0
2
0
1
0
0
0
17.4
141.01
152.57
153 „ 61
0
0.18
91
0
0.25
0
0
0
0
0
1.56
10
1.95
7
40
0
0
0
0
0
0
0
0
0
0
0
0.27
0.24
1
0.02
0.25
0
0
2
0
1
0
0
0
17.4
141.01
152.57
153.61
0
0 . 12931
68.25267
0
0.13595
0
0
0
0
0
1.1977
0.25356
0.04944
0.63806
2.56869
0
0
0
0
0
0
0
0
0
0
0
0.16695
0.15089
0.66156
0.00651
0.00801
0
0
0.01669
0
0.69188
0
0
0
2.86678
73.27466
74.72592
75.65589
0
0.12931
68.25267
0
0.13595-
0
0
0
0
0
1.1977
0.25356
0.04944
0.63806
2.56869
0
0
0
0
0
0
0
0
0
0
0
0.16695
0.15089
0.66156
0.00651
0.00801
0
0
0.01669
0
0.69188
0
0
0
2.86678
73.27466.
74.72592
75.65589
0
                           B-54
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS  (g/Mg pulp) (CONTINUED)
Compound Names

Methanol
Carbon tetrachlbride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1, 1, 1-Trichloroetane
2, 4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acetaldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltriaulfide
Carbon diaulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
155

3.2
0
0.8,
27
225
823
1542
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.17
0
0
0
0
0
0
0
0.03
0
0
0
0
4.2
4.2
2594.264
2617
156 157 158 159 160
0.064
3.2
0
0.8
69
245
823
1542
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.17
0
0
0
0
0
0
0
0.03
0
0
0
0
4.2
4.2
2614.264
2679
0.12
3.2
0
0.2
69
245
823
1542
1.16
0
0
0
0
. 0
0
0
0
0
0
0
0
0
0
0
0
0.0005
0.631
0
0
0
0
0
0
0
0.008
0
0
0
1490
4.0395
4.0395
4105.32
2679
0.12
3.2
0
0.2
69
245
823
1542
1.16
0
0
0
0
0
0
0
0
0
0
0
0
" 0
0
0
0
0.0005
0.631
0
0
0
0
0
0
0
0.008
0
0
0
1490
4.0395
4.0395
4105.32
2679
0
0
0
0
95.7
3.3
2.2
0.33
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
o •
0
0
0
0
0
0
0
0
0
0
0
0
5.83
101.53
0
h 0
0
0
95.7
3.3
2.2
0.33
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
5.83
101.53
                          B-55
-------
TABLE B-8.  EMISSION TACTORS FOR' INDIVIDUAIT SOURCES- AND
            COMPOUNDS  (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulf ide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
161 | 162 | 163 [ 164 | 165
4
500
0
2
6.7
16.1
26.5
21.8
0.1
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.002
3
0.22
0
0
0
0
0
0
0.06
0
0
0
400
505.282
505.282
973.782
71.1
4
500
0
2
6.7
16.1
26.5
21.8
0.1
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.002
3
0.22
0
0
0
0
0
0
0.06
0
0
0
400
505.282
505.282
973.782
71.1
1.2
590
0
1.2
98
113
101
18.3
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
• o
0
0
0
34
591.2
591.2
858.7
330.3
1.6
100
0
2.2
0
113
101
18.3
0.01
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.1
0
0.03
1
0.2
0
0
0
0
0
0
1
0
0
0
4
104.43
104.43
342.44
232.3
1 . 51742
6.21319
0
2.4105
53
75
2422
1469
263.1999
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.09954
0.70248
0.24382
1.57845
0
0
4.24162
85
0
0
0
0.34563
2.22346
0
0
33.04327
102.2567
102.2567
4366.819
4019
166
0 . 04
0.24
0
0.1
53
75
2422
1469
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.001
0.035
0
0
0
0
0
0
0
0.017
0
0
0
0
0.393
0.393
3966.433
4019
                           B-56
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS  (g/Mg pulp) (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2, 4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acetaldehyde
P ropionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltriaulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
169
1
91
0
7
53
1125
533
661
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
2
0.184
0
0
0
0
0
0
0.5
0
0
0
0
100.684
100.684
2420.684
2372
170
0.16
3
0
0.1
53
1125
533
661
77
0
0
0
0
0
0
0
0
0
0
0
0
0
0
10
3
0.0006
0.4
0
0
0.0001
0
0
0.0004
0
0.00017
0
0
0
2500
3.50087
3.50087
4912.661
2372
171 172
2.9
590
0
22
98
113
101
18.3
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
7
0
0
0
0
0
0
0
1.7
0
0
0
340
620.7
620-.7
1195.9
330.3
4.3
346
0
14
98
113
101 '
18.3
30
0
0
0
0
0
0
0
0
0
0
0
0
0
0
4.8
0
0.013
9.6
2.2
0
0
0
0
0
0
0.44
0
0
0
34
372.253
372.253
677.653
330.3
175
5 .05806
20.71063
0
8.03501
0
0
0
0
600
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.3
2.34161
0.81272
5.26149
0
0
6
51
0
0
0
1.15209
3
0
0
110.1442
95.97194
95.97194
813.8158
0
176
7.25722
31.06594
0
3.21401
0
0
0
0
870
0
0
0
0
0
0
0
0
0
0
0 '
0
0
0
600
2.92701
0.43345
0.18415
0.13808
0
243
300
0
0.021
0
0.69125
0
0
0
550.7212
578.7269
578.7269
2609.653
0
                          B-57
-------
TABLE B-8.  EMISSION FACTORS FOR"INDIVIDUAL  SOURCES AND=
            COMPOUNDS  (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2, 4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acetaldehyde
P ropionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
177
23
100
0
25
53
788
533
10
200
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.1
1.6
3
20
0
0
2
17
0
0
0
5
1
71
1
100
174
174
1900.7
1456
178 181 182 18J
33
150
0
10
53
788
533
661
290
0
0
0
0
0
0
0
0
0
0
0
0
0
0
200
2
1.6
0.7
0.56
0
81
100
0
0.007
0
3
0
71
0
500
346.86
346.86
3424.867
2106
0.512
2.22926
0
0.5503
0
0
.0-
0
3.04156
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.00166
0.03129
0.06641
0.44309
0
0
0.02526
0.00543
0
0
0
0.11117
0.01236
0
0
2.02718
3.44328
3'. 44328
9.05697
0
0.73461
3.34388
0
0.22012
0 •
0
0
0
4.41026
0
0
0
0
0
0
0
0
0
0
0
0
0
0
3.31062
0.03911
0.03542
0.01551
0.01243
0
1.02312
0.03195
0
0.00004
0
0.0667
0
0
0
10.13588
4.74913
4.74913
23.37965
0
11
176
0
7
0
45
116
59
200
0
0
0
0
0
0
0
0
0
0
0
0
0
0
35
4
0.07
3.6
0.4-
0
0.4
0
0
9
0
2
0
0
0
954
189.47
189.47
1622.47
220
184
37.98302
186.3905
0
7.26621 ~
0
45.3
116
59
13.36248
0
0
0
0
0
0
0
0
0
0
0
0
0
0
12.22611
0.28222
1.42378
0.6454
0.55885
0
2.30664
0.0324
0
0.00005
0
3.25619
0
0
0
94.76082
201.88
201.88
580.7947
220.3
                           B-58
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2, 4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
185
0 . 2
20
0
0.85
823
638
533
1542
8.5
0
0
0
0
0
0
0
0
0
0
0
0
0
0
3.7
0
0
0.097
0
0
0
0
0
0
0
0.04
0
0
0
2640
20.987
20.987
5386.387
3536
186 187 188 189 190
0.007
1.4
0
0.006.
823
638
533
1542
3.9
0
0
0
0
0
0
0
0
0
0
0
0
0
0
2.8
0
0.3
0.014
0
0
0
0
0
0
0
0.03
0
0
0
348
1.75
1.75
3069.457
•3536
10
3000
0
30
364
126
22.4
12.3
1
0
0
0
0
0
0
0
0
0
0
0
0
0
0
1
0
0
7
0.5
0
0
0
0
0
0
5
0
0
0
0
3042.5
3042.5
3215.2
524.7
3.9
150
0
7.7
364
126
22.4
12.3
3.7
0
0
0
0
0
0
0
0
0
0
0
0
0
0
3.4
0
2
4
2
0
0
0
0
0
0
5
0
0
0
200
170.7
170.7
542.4
524.7
2.5
615
0
6.9
195
42.1
21.5
5.46
0.13
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.11
1.3
0.15
0
0
0
0
0
0
5.2
0
0
0
9.3
628.66
628.66
709.65
264.06
0.975
30.75
0
1.771
195
42.1
21.5
5.46
0.481
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.74286
0.6
1— °
0
0
0
0
0
5.2
0
0
0
Q
39.06386
39.06386
109.5799
264.06
                          B-59
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL! SOURCES AND
            COMPOUNDS  (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1, 1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
P r opionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon disulfide
Total HC
Other
Total HAP
•Total VOC
TRS
EP Codes
191 192
0
4.72202
0
7.90645
0
0
0
0
123.704
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.16254
1.02599
0.73969
0
0
0
0
0
0
4.12679
0
0
0
0
18.68348
18.68348
142.3874
0
1
50
0
0.2
0
0
0
0
1:4
0
0
0
0
0
0
0
0
0
o •
0
0
0
0
0.7
0
0
0
0
0
0
0
0
0
0
0
0
0
0
89
50.2
50.2
142.3
0
193 194 19'/ 198
73
76
0
82
0
0
0
0
94
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
2
13
10
0
0
0
0
0
0
59.7
0
0
0
0
242.7
242.7
409.7
0
73
76
0
82
0
0
0
0
94
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
2
13
10
0
0
0
0
0
0
59.7
0
0
0
0
242.7
242.7
409.7
0
0 . 5
100
0
1
0
0
0
0
0.03
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
1
50
0.01
0
0
0
0
0
0
2
0
0
0
0
154.01
154.01 '
154.54
0
10
40
0
0.1
o-
0
0
0
10
0
0
0
0
0
0
0
0
0
0
0
o •
0
0
6
0
0.02
0.15
0.4
0
0
0
0
0
0
2
0
0
0
0
42.67
42.67
68.67
0
                           B-60
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl 3ulfide
Dimethyl diaulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2, 4, 5-Trichlorophenol
PCP-EF
2,4, 6-Triehlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acetaldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon diaulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
199 200 201 202 203
0 . 19792
11.80506
0
0.28926
27
225
0.246
0
526.3998
0
0
0
0
0
0
0
0
0
0
0
0
0
0
298.6056
0
1.78799
0.03157
0.01405
0
8.48324
0
0
4300
0
0.06913
0
0
0
0
22.4803
22.4803
5372.93
252.246
0.19792
11.80506
0
0.28926
27
225
5
0
526.3998
0
0
0
0
0
0.
0
0
0
0
0
0
0
0
298.6056
0
1.78799
0.03157
0.01405
0
8.48324
0
0
4300
0
0.06913
0
0
0 .
0
22.4803
22.4803
5377.684
257
0.19792
11.80506
0
0.28926
53
75
0.007
0
526.3998
0
0
0
0
0
0
0
0
0
0
0
0
0
0
298.6056
0
1.78799
0.03157
0.01405
0
8.48324
0
0
4300
0
0.06913
0
0
0
0
22.4803
22.4803
5222.691
128.007
0.5
70
0
0.04
53
75
0.007
0.008
1
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.03
0
0.005
1
0.06
0
0.005
0
0
14
0
0.004
0
0
0
87
71.114
71.114
246.659
128.015
0 . 2
20
0
0.85
0
0
550
0
8.5
0
0
0
0
0
0
0
0
0
0
0
0
0
0
3.7
0
0
0.097
0
0
0
0
0
0
0
0.04
0
0
0
2640
20.987
20.987
3223.387
550
204
0.007
1.4
0
0.006
0
0
550
0
3.9
0
0
0
0
0
0
0
0
0
0
0
0
0
0
2.8
0
0.3
0.014
0
0
0
0
0
0
0
0.03
0
0
0
348
1.75
1.75
906.457
550
                          B-61
-------
TABLE B-8.   EMISSION FACTORS FOR' IND-IVIDUAL SOURCES AND
             COMPOUNDS  (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl diaulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Fur an
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS

206

190
0
3
53
788
0.01
0
400
0
0
0
0
0
0
0
0
0
0
0
0
0
0
300
0
22
0.4
0.19
0
4
0
0
860
0
1
0
0
0
0
220.59
220.59
2571.6
841.01
EP Codes
207
3
190
0
3
53
788
0.01
0
400
0
0
0
0
0
0
0
0
0
0
0
0
0
0
300
0
22
0.4
0.19
0
4
0
0
860
0
1
0
0
0 .
0
220.59
220.59
2571.6
841.01
210
0.19792
11.80506
0
0.28926
0
0
0
0
526.3998
0
0
0
0
0
0
0
0
0
0
0
0
0
0
298.6056
0
1.78799
0.03157
0.01405
0
8.48324
0
0
4300
0
0.06913
0
0
0
0
22.4803
22.4803
5147.684
0
211
0.19792
11.80506
0
0.28926
0
0
0
0
526.3998
0
0
0
0
0
0
0
0
0
0
0
0
0
0
29.8.6056
0
1.78799
0.03157
0.01405
0
8.48324
0
0
4300
0
0.06913
0
0
0
0
22.4803
22.4803
5147.684
0
212
0.3
50
0
0.2
98
113
101
18.3
0.5
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.5
0
3
0.01
0.05
0
0.004
0
0
0.3
0
0.5
0
0
0
70
53.764
53.764
357.664
330.3
213
0.3
50
0
0.2
98
113
101
18.3
0.5
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.5
0
3
0.01
0.05
0
0.004
0
0
0.3
0
0.5
0
0
0
70
53.764
53.764
357.664
330.3
                            B-62
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sul£ide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acetaldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon diaulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
216
2
300
0
0.4
0
0
0
0
4
0
0
0
0
0
0
0
0
0
0
0
0
0
0
4
0
4
0
0.3
0
0
0
0
0
0
2
0
0
0
638
306.7
306.7
954.7
0
217
2
300
0
0.4
0
0
0
0
4
0
0
0
0
0
0
0
0
0
0
0
0
0
0
4
0
4
0
0.3
0
0
0
0
0
0
2
0
0
0
638
306.7
306.7
954.7
0
218
4.81615
4.72202
0
7.90645
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.13004
1.02599
0.73969
0
0
0
0
0
0
4.14753
0
0
0
0,
18.67172
18.67172
23.48787
0
219
1
50
0
0.2 -
0
0
0
0
1.4
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.7
0
0
0
0
0
0
0
0
0
0
0
0
0
0
89
50.2
50.2
142.3
0
220
73
76
0
82
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
1.6
13
10
0
0
0
0
0
0
60
0
0
0
0
242.6
242.6
315.6
0
221
73
76
0
82
0
0
0
0
0
0
0
0
0
0
0 .
0
0
0
0
0
0
0
0
0
0
1.6
13
10
0
0
0
0
0
0
60
0
0
0
0
242.6
242.6
315.6
0
                          B-63
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS  (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl aulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltriaulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
228 229
4 . 81615
4.72202
0
7.90645
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.13004
1.02599
0.73969
0
0
0
0
0
0
4.14753
0
0
0
0
18.67172
18.67172
23.48787
0
4.81615
4.72202
0
7.90645
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.13004
1.02599
0.73969
0
0
0
0
0
0
4.14753
0
0
0
0
18.67172
18.67172
23.48787
0
230
0.0066
0.02
0
0.00011
o -
0
10
0
0.00025
0
0
0
0
0
0
0 .
0
0
0
0
0
0
0
0.0077
0
0.00014
0.00024
0.00001
0
0.00012
0
0
0.00012
0
0.0025
0
0
0
0
0.02312
0.02312
•10.. 03779
10
231
0.0066
0.02
0
0.00011
0
0
10
0
0.00025
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.0077
0
0.00014
0.00024
0.00001
0
0.00012
0
0
0.00012
0
0.0025
0
0
0
0
0.02312
0.02312
10.03779
10
232
1.5
28
0
0.2
53
788
533
661
300
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.00004
0.001
0.0005
0
0
0
0
0.17
0
0.01
0
71
0
0
28.21154
28.21154
2382.882
2106
233
1.5
28
0
0.2
53
788
533
661
300
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.00004
0.001
0.0005
0
0
0
0
0.17
0
0.01
0
71
0
0
28.21154
28.21154
2382.882
2106
                           B-64
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS (g/Mg pulp) (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1, 1, 1-Trichloroetane
2, 4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acetaldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
301
1 . 09782
0.24236
0
1.54827
0
0
0
0
0.065
0.01344
0
1.5
1.79168
3.96728
0
0
0
0
0.15
0
0
0
0
0.00942
0
0.08832
0
0.04061
0
2.5
0
0
0.5
0
0.00192
0
0
0
0.77484
10.33044
10.34388
10.83584
0
302 303 304 3Ub 306
1 . 09782
0.24236
0
1.54827
0
0
0
0
0.065
0.01344
0
1.5
1.79168
5.27608
0
0
0
0
0.15
0
0
0
0
0.00942
0
0.08832
0
0.04061
0
2.5
0
0
0.5
0
0.00192
0
0
0
0.77484
11.63924
11.65268
12.14464
0
15
3.5
0
15
0
0
0
0
0.065
0.2
0
1.5
2.5
3.96728
0
0
0
0
0.15
0
0
0
0
0.01
0
1
0
0.5
0
2.5
, 0
0
0.5
0
0.025
0
0
0
2
29.14228
29.34228
44.06728
0
15
3.5
0
15
0
0
0
0
0.065
0.2
0
1.5
2.5
5.27608
0
0
0
0
0.15
0
0
0
0
0.01
0
1
0
0.5
0
2.5
0
0
0.5
0
0.025
0
0
0
2
30.45108
30.65108
45.37608
0
10 . 77623
2.6251
0
8.15671
0
0
0
0
0.00343
0.15355
0
0.03803
0.22788
0.25477
0
0
0
0
0.00209
0
0
0
•0
0.0007
0
0.61834
0
0.33078
0
0.08012
0
0
0.00417
0
0.0173
0
0
0
0.32951
12.31309
12.46664
23.19716
0
10.77623
2.6251
0
8.15671
0
0
0
0
0.00343
0.15355
0
0.03803
0.22788
0.33882
0
0
0
0
0.00209
0
0
0
0
0.0007
0
0.61834
0 •
0.33078
0
0.08012
0
0
0.00417
0
0.0173
0
0
0
0.32951
12.39714
12.55069
23.28121
0
                          B-65
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl digulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1, 1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpiriol
Acrolein
Acet aldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon disulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
307
3 . 11048
2.70061
0
3.25137
0
0
0
0
0
0
0
0
2.29335
1.97827
0
0
0
0
0
0
0
0
0
0
0
0.09274
0.09085
0". 04873
0
3
0
0
0.5 .
0
0.20345
0
0
0
0
13.65937
13.65937
14.9765
0
308 309
3.11048
2.70061
0
3.25137
0
0
0
0
0
0
0
0
2.29335
1.44816
0
0
0
0
0
0
0
0
0
0
0
0.09274
0.09085
0.04873
0
3
0
• 0
0.5
0
0.20345
0
0
0
0
13.12926
13.12926
14.44639
0
42.5
39
0
31.5
0
0
0
0
0
0
0
0
3.2
1.97827
0
0
0
0
0
0
0
0
0
0
0
1.05
1.05
0.6
0
3
0
0
0.5
0
2.65
0
0
0
0
84.02827
84.02827
123.8283
0
310 311 312
42.5
39
0
31.5
0
0
0
0
0
0
0
0
3.2
1.44816
0
0
0
. 0
0
0
0
0
0
0
0
1.05
1.05
0.6
0
3
0
0
0.5
0
2.65
0
0
0
0
83.49816
83.49816
123.2982
0
30.53266
29.25114
0
17.1291
0
0
0
0
0
0
0
0
0.29169
0.12704
0
0
0
0
0
0
0
0
0
0
0
0.64925
0.66016
0.39694
0
0.09615
0
0
0.00417
0
1.83349
0
0
0
0
50.43496
50.43496
80.6801
0
30.53266
29.25114
0
17.1291
0
0
0
0
0
0
0
0
0.29169
0.093
0
0
0
0
0
0
0
0
0
0
0
0.64925
0.66016
0.39694
0
0.09615
0
0
0.00417
0
1.83349
0
0
0
0
50.40092
50.40092
80.64606
0
                           B-66
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS  (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2, 4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene •
Formaldehyde
Acetophenol
Dimethyltrisulfide
Carbon di sulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
313
3 . 11048
2.70061
0
3.25137
0
0
0
0
0
0
0
0
2.29335
1.97827
0
0
0
0
0
0
0
0
0
0
0
0.09274
0.09085
0.04873
0
3
0
0
0.5
0
0.20345
0
0
0
0
13.65937
13.65937
14.9765
0
314 315
3.11048
2.70061
0
3.25137
0
0
0
0
0
0
0
0
2.29335
1.44816
0
0
0
0
0
0
0
0
0
0
0
0.09274
0.09085
0.04873
0
3
0
0
0.5
0
0.20345
0
0
0
0
13.12926
13.12926
14.44639
0
42.5
39
0
31.5
0
0
0
0
0
0
0
0
3.2
1.97827
0
0
0
0
0
0
0
0
0
0
0
1.05
1.05
0.6
0
3
0
0
.0.5
0
2.65
0
0
0
0
84.02827
84.02827
123.8283
0
316 317 318
42.5
39
0
31.5
0
0
0
0
0
0
0
0
3.2
1.44816
0
0
0
0
0
0
0
0
0
0
0
1.05
1.05
0.6
0
3
0
0
0.5
0
2.65
0
0
0
0
83.49816
83.49816
123.2982
0
30.53266
29.25114
0
17.1291
0
0
0
0
0
0
0
0
0.29169
0.12704
0
0
0
0
0
0
0
0
0
0
0
0.64925
0.66016
0.39694
0
0,09615
0
0
0.00417
0
1.83349
0
0
0
0
50.43496
50.43496
80.6801
0
30.53266
29.25114
0
17.1291
0
0
0
0
0
0
0
0
0.29169
0.093
0
0
0
0
0
0 .
0
0
0
0
0
0.64925
0.66016
0.39694
0
0.09615
0
0
0.00417
0
1.83349
0
0
0
0
50.40092
50.40092
80.64606
0
                          B-67
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS  (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl sulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2,4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acet aldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltriaulfide
Carbon diaulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
401
0
4.72202
0
7.90645
0
0
0
0
123.704
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.16254
1.02599
0.73969
0
0
0
0
0
0
4.12679
0
0
0
0
18.68348
18.68348
142.3874
0
402 403 404 405 406
1
50
0
0.2
0
0
0
0
1.4
0
Q
0
0
0
0
0
0
0
0
0
0
0
0
0.7
0
0
0
0
0
0
0
0
0
0
0
0
0
0
89
50.2
50.2
142.3
0
73
76
0
82
0
0
0
0
94
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
2
13
10
0
0
0
0
0
0
59.7
0
0
0
0
242.7
242; 7
409.7
0
73
76
0
82
0
0
. 0
0
94
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
2
13
10
0
0
0
0
0
0
59.7
0
0
0
0
242.7
242.7
409.7
0
6.22096
12.63751
0
7.83702
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.18548
0.18171
0.09747
0
6
0
0
1
0
0.4069
0
0
0
0
27.34609
27.34609
34.56705
0
6.22096
11.73949
0
7.67144 '
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.18548
0.18171
0.09747
0
6
0
0
1
0
0.4069
0
0
0
0
26.28249
26.28249
33.50345
0
                           B-68
-------
TABLE B-8.  EMISSION FACTORS FOR INDIVIDUAL SOURCES AND
            COMPOUNDS (g/Mg pulp)  (CONTINUED)
Compound Names
Acetone
Methanol
Carbon tetrachloride
Methyl ethyl ketone
Hydrogen Sulfide
Methyl mercaptan
Dimethyl aulfide
Dimethyl disulfide
Alpha pinene
Hydro Chloric Acid
Chlorine
Chlorine dioxide
Methyl chloride
Chloroform
1 Benz
Phenol
Dioxin
Furan
1,1, 1-Trichloroetane
2, 4, 5-Trichlorophenol
PCP-EF
2,4, 6-Trichlorophenol
Chlorophenol
Beta Pinene
Alpha Terpinol
Acrolein
Acetaldehyde
Propionaldehyde
DACETON-EF
Toluene
Hexane
Chloromethane
p-Cymene
p-Dichlorobenzene
Formaldehyde
Acetophenol
Dimethyltriaulfide
Carbon di aulfide
Total HC
Other
Total HAP
Total VOC
TRS
EP Codes
407
0
59.21163
0
34.38898
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
1.29851
1.32032
0.79388
0
0.1923
0
0
0.00835
0
3.66699
0
0
0
0
100.8726
100.8726
100.881
. 0
408 409 410
85
85.87418
0
64.4519
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
2.1
2.1
1.2
0
6
0
0
1
.. 0
5.3
0
0
0
0
167.0261
167.0261
253.0261
0
85
86.7722
0
64.61748
0
0
0
0
0
0
0
0
•0
0
0
0
0
0
0
0
0
0
0
0
0
2.1
2.1
1.2
0
6
0
0
1
0
5.3
0
0
0
0
168.0897
168.0897
254.0897
0
61.06531
59.15395
0
34.37835
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
1.29851
1.32032
0.79388
0
0.1923
0
0
0.00835
0
3.66699
0
0
0
0
100.8043
100.80'43
161.878
0
                          B-69
-------
B.12   REFERENCES

1.    Roy F. Weston, Inc.  Field Test Data Summary for Site 4.
     Prepared for the U.S. Environmental Protection Agency.
     Research Triangle Park, NC.  December 1992.

2.    Radian Corporation.  Calculation Sheet, Job No. 239-026-60,
     Model Wastewater Flow Rates, Pulp and Paper NESHAP.
     Prepared for the U.S. Environmental Protection Agency.
     Research Triangle Park, NC.  December 29, 1992.

3.    Radian Corporation.  Calculation Sheet, Job No. 239-026-60,
     Model Wastewater Collection and Treatment Plant for the Pulp
     and Paper Industry, Pulp and Paper NESHAP.  Prepared for the
     U.S. Environmental Protection Agency.  Research Triangle
     Park, NC.  December 28, 1992.

4.    Memorandum from Allen, C. Research Triangle Insitute, to
     Manning, E., EPA.  Emission factors from wastewater
     collection and treatment system at pulp and paper mills.
     April 15, 1993.

5.    Ref. 2.

6.    Telecon. Conference call, Radian Corporation with U.S.
     Environmental Protection Agency.  December 1992.
     Description of weak black liquor storage tanks at pulp and
     paper facilities.

7.    U.S. EPA (Environmental Protection Agency).  Environmental
     Pollution Control, Pulp and Paper Industry, Part I, Air.
     Publication No. EPA-625/7-76-001.  Research Triangle Park,
     NC.  1976.

8.    Memorandum from Gideon, L., and Olsen, T., Radian
     Corporation, to Lassiter, P., EPA/CPB.  February 5, 1993.
     Emission factor and model process unit revisions for the
     pulp and paper NESHAP.

9.    Memorandum from Olsen, T., Radian Corporation, to Lassiter,
     P., EPA/CPB.  April 5, 1993.  Totally chlorine free model
     process unit for the pulp and paper NESHAP.

10.  Research Triangle Institute.  Hazardous Waste Treatment,
     Storage, and Disposal Facilities:  Air Emission Models.
     Draft Report.  Prepared for U.S. Environmental Protection
     Agency, Office of Air Quality Planning and Standards.
     Research Triangle Park, NC.  April 5, 1987.
                               B-70
-------
11.  Research Triangle Institute.  Emission Factor Development
     for the Pulp and Paper NESHAP.  contract No. 68-D10118.
     Prepared for U.S. Environmental Protection Agency.  Research
     Triangle Park, NC.  October, 1993.
12.   Ref. 11.
                              B-71
-------
           APPENDIX C

       MODEL PROCESS UNITS
C.I  Pulping Model Process Units
C.2  Bleaching Model Process Units
C.3  Definition of Terms and References
-------
                         APPENDIX C.I
                  PULPING MODEL PROCESS UNITS

     This appendix presents emission points, emission factors,
and vent and wastewater stream characteristics for each of the
18 pulping model process units (MPU's) presented in
Chapter 4.0.  The model process units are defined based on
pulp type, wood type, digester type, washer type, and whether
oxygen delignification is used (see following summary table).
The following figures (P1-P18) represent the emission points
associated with each model process.   Tables following each
figure identify the emission points within the model and the
associated emission factors and process vent and wastewater
stream characteristics of each emission point in the model
process unit.  These characteristics include:
     •    Flow rate factor; and
     •    Hazardous air pollutant concentration.
     The assumptions and derivation of the emission factors
are presented in Appendix B.
     The following example presents how a model process unit
would be assigned (or "mapped") to a pulp mill.  Assuming a
Kraft pulping mill with a batch line pulping hardwood
(1,000 tons per day) and a continuous line pulping softwood
(1,000 tons per day), two pulping model process units would be
assigned to represent the two pulping lines.  The batch,
hardwood line utilizes a rotary vacuum drum brownstock washer
and no oxygen delignification.  Using the summary table as a
guide, the batch process would be assigned model process
unit P-l.  The continuous line utilizes a diffusion washer and
                            C-l
-------
oxygen delignification.  Using the summary table as a guide,
this process would be assigned model process unit P-12.
Definition of terms and references are presented in
Appendix C.3.
     The emissions from either process may then be estimated
using the appropriate figures and tables.  For example, the
methanol emissions from the Kraft batch process (Model P-l)
rotary vacuum drum washer would be estimated using the
following steps:
     1.   Identify emission point code (EP_CODE):  for
          Model P-l, the code for the washer is 177;
     2.   Identify the associated emission point emission
          factor ("Compound"_EF):  for methanol (MEOH_EP), the
          factor is 0.1 kg/Mg pulp;
     3.   Multiply factor by process line capacity:

      0.1 Kg MeOH   1000 Ton Pulp     1 Mg    90.9 Kg MeOH
      ^^•HI^^^MIK^^^MMBH^^^M^B^M ^^ ^^•••^^^^••K^^^^BHH^^^BIBBH^^^ ,/fe ^^MM^^^MMB^^^HB ^™ _^^^^HM^^^BB^M«I«^^B^BW«^
        Mg Pulp          Day        1.1 Ton        Day

     4.   Convert to annual emissions, assuming mill operates
          350 days per year:
             90.9 Kg MeOH    350 Day _ 31,800 Kg MeOH
                 Day        1 Year         Year
                              C-2
-------
CO
EH
H
CO
CO
W
CJ

P
04
W
Q
i

i
H
(J
CQ

g
CO
c
o
4J 0*
id z
£ o
c a
•^ ?^
« ""
•o


f
Washer

-H >»
U 0

S M
U K
•°«
0 >•



P
Q

$
0;
>i
4J
C
"a
^•1
3


•
S **
O S
t* «7
04




o
z






•o
Rotary



*2

•O
id
X


U
id
CO











1-1
1





i S




o»
c
If
Rotary
proved
e
M


**4 &*«

*> -o
0 id
01 X
o
a
Batch
ntinuo
S




Li Lt
M M




«N n
a. Oi





O 0
z z





c
1 ^
3
Rotary
proved
e
M


K ^4

•O *J
. >1
u u
id id
4J *J
S S

4)
^ w

01
•0 4>
U  0»
c e
-i ~i
as jd
n o
•o -o
2 §1
2 S
a 04
e s
M M

W W


•0 +a
tj tU
« 0
X 01
a n
S S
ntinuo
ntinuo
S S




< id
Li LJ
M M




^ CM
1 1
Oi a,





o n
4) 4)




O^ 0^
c e
-- i -i
O 0
3 3
•a -a
§: §:
S 2
Oi Oi
8 S
M M


US £^

•0 *J
id o
X CO


£ JS
u a
-u *J
« «
00 CO





« i
U 14
id «
JJ *J
S S

4) 4)
i-l i-4
3 3
01 01
•0 4J
id 0
X oi


JB JS
U U
4) JJ
id id
ca n




4> 41
^ ^
3 3
01 01




in vo
Oi Oi





O 0
z z




O^ 0^
c c
••4 -^
o o
id id
•O T3
4) 4)
> >
O 0
o\ 'a
S S
M M

id id
•** itf

•0 *J
« 0
X 01


JS JS
u u
4J -U
id «
CO 00





id «
X X




f 00
04 Ol





























41

id
u
Oi
Oi
o
z
H
Z
id
                                                                                                                      • A  ~4
                                                                                                                       I  I
                                                                                                                     •*! O -*
                                                       C-3
-------
                                              cc
                                              CD

                                              Q


                                              X


                                              cc
                                              £
                                               I

                                              .0


                                              _o
                                              H^

                                              c
                                              0)
                                              O)
                                              CL
                                              Q_
                                              0)
                                              3
                                              O)
                                              IT
C-4
-------
 **££$*
         ??
ii


                                         — 0--OM — 0 o'~
                                         **
                                        r«i«>'*«*-O'in.nKiN.»-
                                           
-------
                                               O

                                               "co
                                               CD


                                               cf
                                                2
                                               x.
                                                i

                                                g


                                               8
                                                0)

                                               2

                                                O)
                                                c
                                               o_
                                               CL

                                                0)

                                                3
C-6
-------

1 1
§ i
i'! !? 5!

a, -o »•• (^ art «~ o *o 2
< m •« >* O «O 2 -*  | «, ^ - » » 0. - «• ~
a.
3 , ZSSSSSSZSslsS


UJ
1
o •— «n *-
u
UJ
i
s sssasssssssss

a.
a. acacixaeatacacacatiaeoifKac
S ----------«-«
Ul
a.
i -*.j.^ww_j,j_j.j.j,j^-j

£
•i
* £
4i C 41 U <
1 $ 1 •
3 > 3 o o "o ui >uu*9
**O**^— Q^^B —
.2 . -0-0! I a i .-.-.•-
! " S s s « * s. ". 2 2 s s
g^SS 333Sg333SSS
a' !
T
P O.O.O.O.O.O.O.O.O.O.O.O.O.













X


s
2
i
M
w
u>
2*
I









"7"
y
UJ
-'
***(
S
tu
ii
V
UJ
U
"'l
^

X


u.
§

M
1!
M.
UJ
U4
U
„.
s1
*

***!
3
5
SOUftCE
UJ
§
u
u*
!












« ^M»«m^«^mmm
£ §§££££§§§*§




§ ££££££§§££§
«i ^,^-m-M^or.^^


„ ^^^^^w-^^^.v,
iS 899S!9!3(;!9S!«8

* g^2*S*g|e^

8
u S I
* * X
U £ U • M « C 91
. u g at « S <
nils = • : s
i ^ i ! i I s ^ \ - 1 » :
hln:>s|!hl
«»OW«*«>QIQMB —
s . •» •» 1 1 a 1 .- - .- -
I " 1 •• • .•ca'~fefeSS
M->*M..i.« *.»*M>*.M<
mssss-kiii*
s=.S-*i||lllh
aV*~*OOM333IUJUiu>3
S S3 3 35 SS S S g S S

fyN(V(MNf^NN(MNMNfM
a. a. a. ^0.0.0.0.0.0.0.0.0.
C-7
-------
     3s*i
   i*»  1*1  --^^^^^,-^^rj*
  !I I 2  sssSSc^ccs
a. I 2
!rr
 i!
         M i g jjj
            '
 I
I I*II
    85?
              si
    Ifl=-ll5l£||5
    ipjJijljM.1.!
    f!fB-e-:!*!iSSa
    t5t£2fe5S!:s:2
    :r:i§iiiiuh
    U«U-»-» C44CJ > > >UI
    S—zoax333uuiw3
    82:2222 22 22 2 ££
                               C-8
-------
                 3
CO
p
                   §







o
HI
It.
u_
ID
1
. g
^^
2

I
i

Q.
1
I
  CONTINUOUS
    DIGESTER
                                                                       O)
                                                                       CO
                                                                       I
                                                                       o
                                                                       o.

                                                                       VJ
                                                                       o
                                                                       3
                                                                       _C
                                                                       "c
                                                                       o
                                                                       o
                                                                       Q"
                                                                       X
                                                                       .0
                                                                       16
                                                                       o
                                                                       c
                                                                       CD
                                                                       O)
                                                                       CO
                                                                       Q_
                                                                       03
                                                                       3
                                                                       O)
                              C-9
-------
  "s.
     (Mr*  ~-
         Ss!=
        i
     ii
     ru  O> *> nj    *M fM
     uuiacuiuiuiuiacaeui

        M      (AM
S

5

f
      sss
ss
   |
                                                   :
                                               000 — « — 00^ — o

                                               5 M * * * s * at g a «
                                               ^orfM^OOMry^mff
                                                      •*  <* ^ m
                                                      u  in ^ * in
               s 12
               *- U Of
            -
       J3 J3 S 0 1
          £ w p
      •     s •
             -
           . ?  s   : S
           *• C  W   4- O
           «• * S  ui   *
            5» -o  «   • *
            •* C W U   C U
            • OCM.M  * *
             "
                           Illlllllli
                                                            S
                                . - . * g J 5 S 5
                               e g c j M. B. s | a



                               OOOW33UIUIUI


                               ss^tcsassz
              a.a.o.a.
                                        C-10
-------
3   i
    m
CONTINUOUS

  DIGESTER
t,


2)

MULTI-EFFECT
EVAPORATOR
                                             o
                                             3
                                             O
                                            O

                                            Q"

                                            I
                                            ^
                                             i
                                            c
                                             co
                                             o
                                             0)
                                             O)

                                            'a.

                                            CL
                                            CL


                                            I
                                            O)
                                         I *
                                         l!

                                           I
        C-ll
-------
I
^
           ao tM    in •-  O* » ^ OJ       CM
           umacuuuwuocaeu

           <<<<<<<<<<<
           ocacacaEtvatatatatatac
                                                      '*«*>(NKtf«4^f*l'*rMl


                                                                                                            m K*
                                                                                                            A i
                                                                                                               tel    IA •-  ^-
                                                                                                       •?
                                                                                                       •0
            8  «
                    f  O UJ 5  H  tt t»
             **•    JE O •*>  U  U i.
gase
blow gases
bloM conde
hood vent
ood vent
ECKERS/SCREE
oaai tank
s, v
ensates
ace cond.
STORAGE
rs
rs
DE
fo
tor
tor
ACK
ges
Diges
Diges
Knotte
Uasher
UA
Ua
Ev
Ev
Ev
WE
                                                         SCCfcSS
            22222222222
22222222222

                     "'  C-12
-------
                              Q


                              O)

                              11
                              ~ o
                              s
                              gg
                              I
                              O)
                              U-
                         11
                         * a
                         I!
C-13
-------
 a.1 i s    *  S! s! g s
 « ! rg    -•  -r « 55 -r
       5>S»>>    MM
       <<<«<<<<<<«
       atacoeacacaeacaeacacat
;*;
            a. a, a. a. a. a. a.
i u « S          §S
I « 3 C          u «

i e - u  *   slgl'5i
    aoo^iu   >uoi9
    ** — •— 5 x •     —
     A A O tJ m «  • • ^
§n
s-!
is &
                              I I  I 1 \ 2  I  5
                              U.r.23|S | „.,...=

                              I « I •-• ,- - ° - S S S S

                                            -
     33
    £££££££££££££
                           £££££££££££££
                                          C-14
-------
s
   u.

     !!jggSjj{|8j:j|«jg§gg3j

   2  -*(X»'*r«*>if>i--»*i«^'<><>*
  U




   ®     ^T-lr-lU-l  ,-,-.- ^ ,, r*
   ,_	 _ _ ___ ,_- — __— _—	 _J

           »- 1ft










   i



   i



  I

   i

   a





   i


   IW
   %



il

s

I  %

s  I	






        ni  iv *- ^ W

















     i            :


     |p



     •Ml  »       !|

     ii:  1  s   s!i
     = s ? : I  ^   ; ^ 5



     i.li jljiilij
      .*.-»•" I a !.-.-.-- 1
     l"l«-« .°-Sfefe8-e
     srsssc«;«ssa3«
     jf°J'S2»«ttt!t""











     £££££££££££££
                                      C-15
-------
          UJ
h- LU
S58

        CONTINUOUS

         .DIGESTER
                                                          CO

                                                          O
                                                           c
                                                           o
                                                          O
                                                          4=
                                                          CO
                                                           O


                                                          1
                                                          O)
    3
   D_


   CD
   O,

    0)
    h—

    O)
s!
                                                   i
                                                   S
                                                   3
                     C-16
-------
' I
 «c

i V>
,  I

! S
      •*  Nt
      >  4.

      i  s
      •3  *j
<_)!*

».' i 3!
            ^ S S
 o1 ! s  %  s
 —i *™  ^  o>
              SIS
1-1
  , !    5 - 5  - -   5 5 -
 3' Issssssasssss
       <<<<<<<<<
                       "

                      I *

                      I	
   C - u


   & S 8
                :s
                 ~
 ECO  **
 - u  •



.!.!»!
                         S
       .^ISECCw
       2 * •   .252
                          if .-
«___

« " <* * «
>> o v *• «
(A  (fl M «i i


§5g!l,
3 u g
» • -
                                    2 s a

	h-


 8
 U



 i' ;
                                   C-17
-------
X |
^ I
  I
 s
           3338$
 2222222222222
                                  C-18
-------
                                          Q


                                          CO
                                           ZJ
                                          CO

                                           c
                                           o

                                          1
                                          0)
                                          2

                                          O)
                                          c
                                          o_


                                          I
                                          O)
                                        I
C-19
-------

             ^   •* •-
      s s s! g s   s a
  s s
  9> 


         Ul
     •
    Q    ^
  Wl X    U
  Ul O (A  Ul
  ^ u ui  ^
  <   W) M u.
AP. VE
ANK VE
SES
S
FFE
H- J3 O I/I CA O Ul UI-V»   W

§5»«^M«
MUIUiaaui335$3
KNOTTER, VENT
EVAPORATORS, CONOENSA
EVAPORATORS, SURFACE
DIGESTERS, RELIEF GAS
DIGESTERS. ILOU GASES
EVAPORATORS, MULTI EF
WASHER, HOOD VENT
UASHER, DECKER VENT
DIGESTER, M.OU CONOENSA
WEAK HACK LIQUOR STORA
WASNER, FOAM TANK VENT
Ul O M  Ul     < <
SU!X»£     S 8 5
S S 3 !« "   - S S *
ui <   < —   at M
    ^^Smm^-mm
    M M O Ul UJ M   Ul
    2^iil»2l
    OOiil33o33
                                                  r-20
-------
;




d °-
ii
5 LU
                                        Q


                                        X

                                         CD
                                        CO
                                         I


                                        .o
                                        *•?
                                         CO
                                         o
                                         0)
                                         3
                                        o
                                        a.

                                         0)

                                         =3
                                         C3)
                                    * w

                                    ll
C-21
-------
   ? ?
        ^  ** •-
     o> -* — *-
XIUU1XVV SXUlXX
                      '*-*•*»«'***<*
                                             -a
                      ui  £
                      M CA Ik
                      < UJ Ul
                      UM
VAP
ATES
GE T
         Q ^ 1ft*
        F- 5 Wl >
   • « • -   - =
SURFACE C
LIEF GASE
OU GASES
HULTI EFF
VENT
R VENT
OU CONOEN
OUOR STOR
TANK VENT
VEN
ORS,
TOR,
RS, RE
RS, IL
TOR
IL
LI
                                       8 M M O S S 5
                                       llllll!
SS8SSSSS8SS
sssssssssss
                                  i
                                C-22
sssssssssss
-------
                                         S m
                                         h
                                                c/3
                                                CD
                                                o
                                                o
                                                ns
                                               _o


                                                CD
                                                0)
                                               CO
                                                I


                                                o


                                               1
                                                0)
                                                O)


                                               'a.
                                               O)
                                               Q_

                                                CD

                                                3

                                                O)
C-23
-------
5!
S}
I
                is 8!
           *• fM (M (M
           i + + *
           » s £ s
           ^0 -* •« **
           v m i/> ro
     s  s
I i
     sssssssssas
     35353333533
       zzzzxzzxxz
                              lilil  sl-a-i
                                                    38
                                                 S2 gg 888

i ^ 5
! 21«,
: > H ui
i X U <      tfl
 U  VI   t-  ui
 !»- ui x   m  I-
 < ac ui M  ui  «c
 • = i s _ »  s
 " X O < X M  141
 llaas^i§
 1*1If 3*°
 Ul  -   X O ^UJKMK
  WMMlfuSB
 iS^Slll
 >-xoaw3uiui
ENSA
VENT
TORS, SURFAC
ACK LIQUOR S
NTINE CONDENSE
IATCH VENT
INE CONDENSA
ENSATES
S
VEN
ENSA
VENT
ENSAT
ACE C
STOR
EM, TURPENTI
S, ILOU COND
S. ILOU CASE
. NOOO VENT
FOAM TANK
ORS, VENT
ORS, COHDE
ORS, SURFA
                                              Q IU O M
                                              S  § S
                                              3 x u <
                                               u  t/»
                                              UJ ^ Ul
                                              2 2 =
                                          2s;
                                          1 ^
                                          U H-
                                         M m IS
                                         w q <
                                         »»UdC
                                         a u, 5
                                         22"
YSTEM
OIL
SYSTE
STERS
STERS
TERS
                                                 ?33
                                              »— Q ^ ^ -^ 0 X    ••
                                               .2 . • • 1 i » «• «.- j
                                              5 • 5 « « .S888S
                                              ^^*-««M  » ^ P »- <
                          §i§iiliiiii
                                                          8 $
      itttttt
           £££££££££££
                                      C-24
-------
                                               Q

                                               CO
                                                C/3
                                                C/3
                                                CD
                                                O
                                                O
                                                O
                                               >£^

                                               CO.

                                               15
                                               _g


                                                0)
                                               n
                                                O
                                                I


                                                O
                                               CO
                                                i

                                                O

                                               '•i
                                                O
                                                CD
                                                O)

                                               'a.
                                               O

                                               ol


                                               §
                                               O)
C-25
-------

I
}
t/t
1
SFLO_FAC
o1
a'
ENCLOSURE
a.
C,
Ob
a.
2
UJ
a.
"l
B
a.
Ul
|



\
oi
A. „ ,. ^ ».
3S5 SS

O
i
o t/t S r£ 2
_ _ _ 3 - -
£ £ S! S S S
-

a a a a a s
333323
U U U U U U
M tfl Vt VI Vt VI

22222^
UASHERS, KNOTTER VENT
DIGESTERS, RELIEF GASES
DIGESTERS, ILOU GASES
DIGESTERS. IIOU CONOENSATES
WEAK HACK LIQUOR STORAGE TANK VENT
UASHERS, FOAN TANK VENT
fiSSS S K
<~ fM AJ IM 
-------
I
                                         LU
                                         O
                                         O
                                         UJ
                                         a:
                                         m
0



1 ^
0 ^
JLTI-EFFE
fAPORAT
2 iu
s
CONTINUOUS
 DIGESTER
                                                   # w
                                                   l!
                                                       o
                                                       c
                                                       *-*-rf

                                                       31
                                                         8
                                                       |0

                                                       •  03
                                                       c a
                                                       8
                                                       II
                                                         D.
                                                       - E
                                                       CL
                                                       OJ
                                                       3
                                                       g>
                                                       L_
                         C-27
-------
>
«0
o













1



y
-Jt
haracter
s :
1 -

a.
I













3

i
§
i
(/>
g

*
u
O
V)

o1
*
a.
i <
s
3
01
U !
i i
ft i
1
i
a.
a.
1
Q.
S'
S
UJ
U

s
§
r •
i'





j
i* pn tv
CY ^ i«
ry i*» — o rsi fi rsi oj ^r (M
£* Ssg = SSS5


* +
% & g
O1 O* fNJ
O sj- -*

§J III* iili
~ ~ »»-~ ~-~«-

22«22|SSS2222
W* U) VI

^- ^







iiiiiiiniiii

.
(/>
UJ
1 32
UJ M W >
* i - « s
« ^ " 2 * 2
LU ae • O ui
"— UJ O ^ * U*
< « v» z CD 3  v» u— ujO <
uj x kvz ^~ u v X «
vtwtuj Q uj < 333
«U«Q > gn UJ — — —
<3vtX^gc x Ul » •- wi
w»
— ' O O Q LU >  1 01 3 3
M M u *— uj a <
3UJQ > (/> uj — — •-
1/1 * * • a u •- ^ «i
22*«"w»"cA<'"^^* "
a a a wuuiooaa
ss-esaafessssa


•.•.a.^c«.a.ft»&&&&
C-28
-------
vt
.at

^
O

«,
o

UJ
M
3
u
. ACETOPHNEF
UJ
a
U4
Ul
8
UB
UJ
i
2
M»

ft.
5
UJ
*

£


a
3
8
i'
? ? 7 7 ? 7 7
5 £ S £ 2 a a


9?97?7??77


*s£$S3*i!S5

M •« m
$ jM 3
*- >r *%*

UJ UJ
O •*
O rtJ



O irt S
•O rvj ry

2 1/1 S »« •*
- ^t ^ - N.

S2S *2
« -0 - - -

DIGESTERS. RELIEF CASES
DI«SIERS, M.OU CASES
PlfiCSKRS, M.OU CONDENSATES
KNOIIEIS, NOOD VENI
IMSNERS. SCREENS OR DECKER VENI
UASNERS. FOAM TANK VENT
EVAPORATORS. VENT
EVAPORATORS. COMOENSAIES
EVAPORATORS. SURFACE CONO. CONDENSAIES
OXYGEN KLIGNIFICATION IIOU TANK
o,
?
-------
                              QC
                              O
                              HI
                              DC
                              s

                              I
                              O
                              O
g
111
/•
(
V








s*\
"* /
-/




EFFECT
F
^
^
i
i
i
i
i
i

g
1
2
<
g!
                           ^..rr
CONTINUOUS

 DIGESTER
                                               03
                                               D
                                               O
                                               0-3
                                               I
                                                1 CD
                                               C O)
                                               S £
                                               coO
                                               S d>
                                               c.E
                                               CD ^
                                               2 g
                                                                £1
                                                                 .  Q.
                                                                ^  E
                                                                Q.
                                                                CD
                                                                3
                                                                O)
            C-30
-------
                              H!
 3  rw
                 o o

                 2 °
 < ; fi w\  ry  p-*->-^    f\* ^ w rg

 2' • S S  s  i§§^    3222
       I 1 5
                  5 5
                           I
    (J  Wl'
      (/) Z
      £p—       ^ i—  uj w    «
      » u*  v)  LU x  *- u 3 2 91
      3O * vi uj  uj uj  <  O O O
      u — u> •-  at >  t/» IM — —• ^
                  u »- w M
    isl?
           2 S 5 Z = S !S
           * ° WS « 1 a
           « » « 2 2 - §

5 ± S S 2 S I' -• I I I ** I *
                 m ^ ^ ^ ^
                 S S S S Dl
                            S

                            i 2 S
                            s > <
                            « - S



                            - S S
              i?
             3 " S i S
             tf» W — — "-
— — —  _-^ — ~_^^^*«^aiu
S * S 8 i   2"">55 — "~a

IW  tw M M  .



a < u — — S
a »- * o a x
                                5" S 5" •»•«•• - a = S 9 8 £ ^
                                         > > g g u «|
\  8 ! sl5SS?22l?!22?S
,i_^_;	
i"i*~^.  -
  w  2fr^'Xn«f>JNfM(NN^rvi^(M^fV
  3  iT*"^*"*"*"*"^**"^^*"^*
Lii	'i*"""      fc
                                        C-31
-------
r — 4-
                 a 8 8 as «
                 < — -* — 
-------
                             UJ-
o>
' OXYGEN
	 ' DEUGNIFICATION
BLOW TANK
(



OXYGEN
DEUGNIFICATION



CO

!°§
J

| Hi N


3 * X

S

I


i

8M £
7 U> ^ ^
I O CD*"

uT\
t)
. .......... DAT^LJ
• 	 BATCH
DIGEST!
0 I
$ O
_, 1 §
. IAJ
Liit tr
CO )— f)
	 1 —
i 2
1 UJ
/^ n f*\f<*
J s~\ ' o ( S )( a
\(J ^ v^/v:
T 1 i
^*
(D
r^)

^•" -V "
uj O
II
_ il
/fjrS 	
v5> ^
- 	 O UJ 1
— [---=!¥ 3g2^ i
— r iS5 	 ^m§il. -—___'
M^ ^OO^
^ ^ CIi. "^
1 	 ' g^co

®t

*•••- § 1
s
-

( 8 }
i y^y


-

ER
_ j





!\
)
•J


j£
o
"m
Co
C
Q- o
^ -^=
il
^" c
51
i UJ
Ofl\

CO ^>*
057^
10
§ C3)
•o .£
~- £
O) CO

i^L ^>
3 T3
Q_ 0)
51 c
"• E
0) —
^~
J
O)
iZ


i §
fi
|Il!
i
i
i
i
                                  C-33
-------
i -
5
g
a.
s
i
*
u
o

o1 [
* <
1 a.
i
u
' ^ i
,
u
2
• ft '
g1
s
a. ,
a.
a.
*
a'
a.

,
8
u
a.
i i
1 u,


M
t>
„, , 	 Q
3 — -0 0
a ^ i/s M

*
0
-J-

s Ii§
~ - » »

_ 5 - _ _
uj ac uj u* uj
•"




ac oc at ac ac




iiiii

IGESIERS, RELIEF CASES
IGESIERS. ILOU CONDENSAIES
IGESIERS. ILOU GASES
NOIIERS. HOOO VENI
MSHERS. DECKERS/SCREENS

S3SCS




m n
•- >rt
(\J 1-1
I 2
^ -»

ii
•f •*

**
- «

--55
w LM « at
« Ul




S 5 S S
x x x i




im

MSNERS. FOAM IANK VENI
VAPORAIORS. VENI
VAPORAIORS. CONOENSAIES
VAPORAIORS, SURFACE CONO. CONOENSAIES

2SS 2






PU N * IN
« K S S
CO ^* > •*
F*> K. ^ I/S



iili
(N( i" ry f>j

«-•.«-».
UJ UJ hU Ul





i ill


2 2 S 2

l£2£

M*CEN OELIGNIFICAIION IIOU IANK
MVGEN DELIGNIFICAIION UASHER VENI
CAK ILACK LIQUOR SIORAGE IANK VENI
MSHERS, HOOD VENI

» 5 » 5!

















s
|
w*
u
O
S
§
u
«
'i
IU
M
1










1
1
***!
U
U.
u
*
a
rg
^

w
Si

1
s
-

l'



Ul
UJ
u
I'

IM
tw
*


i
a.
w
Ul
1












U UWI^UWWWUJ^UJW
O ^»5— OJOOSo
„ M^-W^^^^B,^-

>

9SS2SSS!9SsJ898



°g£**3*i**§gg

**S^2§§* *O

w»
u*
3 -3
Z • 111
Ul M Ul >
§!:*
u a * 2
uj • O tfl
< tfi wi X m 3 (S(
(AM Z •» UJ O <
Ul Z UJZ M(JZZK
Wt u* (A kM U* < OOO
SOW Cat > Crt UJ — — 1—
f Wl " U ZU*-»-tA
3 < Z W* M W«««C >-
t*>woiu^.z*-o**-uucKai
IM _>V» u 5* — * 9
uj^wBMC Z 3| w O
• • • l-a 1 » «.-«2 2 - 1
sf s" 8* «.\a- '. 5 5 § s S S .
---£«£«««>>££
WIVIMN* UWOPOUW Ul
3IUIM**XX&&&UtfMV
33oi«i«<22SS53
3S5s3322233if

sss.ezasissssis



                                    C-34
-------
? T 9
   04 fM -O
   2! S *
 Ut        • O M
2!   «s »i"5<
 »WW^XX&£Ct3
 33o3S3S3S
SSS5 13 >!!i
                               C-35
-------
                     UJ
                     C3

   OXYGEN


OBJGNIFCATION


  BLOW TANK
                         o
   OXYGEN


OeUGNIFlCATION
                                             o:
                                             O
                                             o
                                             HI
                                             cc
 o

I
 o
 o
                  o
                  13

                  m c


                  §i
                  0) -^
                  Wi/ «*-

                  4S 'S
                  CC O)
                                                               O  03

                                                              '•=  O)
                                                     U^.    .2  s?
                                                               0)  D5
                                                              s I

                                                               O) W

                                                              Q.

                                                               O)
                   C-36
-------
                            I
                       - -i  I  a
                        1  if
g
o'  o  g 3
s'  S
                        4 I
             ocorocaroracar*
2^222222
                               *  *§£***§£££*£*
                 3  _
                 i 2 £
                 I 2 . S
                 " a * -
                  ' 5 Sc u

                5 u 8 8 8
                VI UJ — — »
1-1
O w Q V
z > a uj
u 5 W *
s : s j
   o.oca.    5 w> < a f « - — Su>
   SEttJflEalal  aewujOP*fc^5>


   Z* ae C*  • •  Su.oe£at~j^S
   UJ  UJVICA*   O Q O Ul UJ U
   iA~>viu«ujoivrvr««E<   wvi
    - -     -«gataeaad)«


             i>>2l§vi

   a. a. o. a. o.
Ut  <           Q Z >
S ; S           15.5

|s|s    M     u?|2

 u  wi    w ^  iw o    <
aSiiSin   « 2  SU88S
                                  &&A»&&&a&
                                     C-37
-------
s .:
    -
9 > Z u
O  O^    Vt
"S8S    2
3( = * 2 >»  £
— 3 •> S tw  u
3 .5 1 2 5 "*
s.SSuas,.

5^S33o =
-§~SigS
                   8 8
                   —
                 .  -S S ^
                                         C-38
-------
   OXYGEN


DELJGNIFICAT1ON


  BLOW TANK
   OXYGEN


DEUGNIFICAT1ON
                                                                d) CO

                                                                £ •-



                                                                IS
                                                                ** 05
                                                                §Q

                                                                '•« c
                                                                « 0)
                                                                .2 O)

                                                                in ^

                                                                51 2


                                                                If
                                                                O)
                           C-39
-------
                        g
   K 3   i* $ £ S  S !« tf *
   >O *>   -O ^ «- Kl  > «3 ^- sT
   Is


        ssssssssg
        znmm
I !
                          ££§£££££§§;£*
        Ut  UJ

        LU  -•

     <  (/>*/»**.

     t/1 W < Urf UJ
               S 2 .
               <  UJ
             M •> 3 Z
             u>  O  X U O VI
             5 sts
322SS232!*Sa3
                                        C-40
-------
§



  'i
   o





   5


   w.  rv \ft






  !



  Ii.

      m

      S

  ! <
  i—

   ",

   8


   Ul

   §'


   UJ




   i
o  —
U  "*l
   2  s -    gjgjgg     ^
   SSom    -*>»«* o     oj
   ^    .     .
   O  -O rti    « •)

.1

   <    
-------
   OXYGEN
DEUGNIFICATION
  BLOW TANK
^
p
   OXYGEN
DEUGNIFICATION
  Co]
s
o
                                       g
                                       01
                                       o
                                       o
                                                             Q

                                                             I I
                                                             ~5 ^

                                                              <=1
                                                             .Q Q
                                                              2 ®
                                                             £ O)
                                                             Io
                                                                .
                                                              .£2
                                                               . T3
                                                              CD «
                                                              51 2
                                                              0> Q.
                                                              51
                                                              O)
                           C-42
-------
»
<%J
i


2
2
z
s
< ] ?y •- o
O t r^J f>J »« ^ ^ ^ ^ *« ^ *
a. (NO uH ^ yfl (^ tpp^CS'
• S , M ^ ^^OT_ ^_».^
u
2 ! S S 5
ui •«» •* •-

ii1 Is iSigts 2982

a- 1
1 =, i » - 5 5 	 5 	

3 M vi vi

^ i
UJ j
a. '

-o ' 8 ! "* "* "* "* "*
ol '
1 :

| S33333S333333
UJ '
! »' 222i22222222i
£
ui
< X »»
trt uj X i—
X > UJ X
o - * x !S
x a, M •*
3 5 5-2
u tfl •— 2 *
UJ O (/i
(AX u < S » 3
UJ O uj i« <
_ ^- u wi *. * * 9 9
ae< ujviu. ujoOO
UJ (^ U4 Wf yj UJ O ^ — ••
->2S3S-5S"'«3
x^fiu. o^kuuacuuta
ujXX*u.-^> O — — X
; 'SSSSgi.gl^^SI
§i»«ss»s"=3§8
x o of at *vu* •M«rf^5
i B*^OO^y>oav»ui«uJX
i «* . S < u* uj 5 -22 -
aujaco|«"-»-9eatk-«xxai
^ujOpvivipujiA uj uj uj
ji ssilaaSsissSSs

1 t t
8 .^

iu i J_ .


















>
I
i
X
$
s
s
«)
(A
'i
UJ
•O
|











I
MCHCDEF
'"l
i

UJ
1
1
u
UJ
U
*
UJ
1
(M
U
u>
X

UJ
*
u.

u.
ul

™l
y
IW
«M
u
».
i'
*

UJ
UJ
*


5
IM
i
">
i

















uuvywwjjvuuvuui uvu
ssa^slisls IS




^I^^^IISIII^




=a«8*8S»88S*8

^^^c^imil^i

NOIIER. NOOD VENI
MSNER. FOAM IANK VENT
VAPORAIORS, CONOENSAIES
VAPORAIORS. SURFACE CONO. CONOENSAIES
IGESIER, RELIEF CASES
ICESIERS, BLOW CASES
VAPORAIORS, NUIII EFFECI EVAP. VENI
MSMER, DECKER VENI
IICESIERS, BLOW CONOENSAIES
CAK BLACK LIQUOR SIORACE IANK VENI
IXYCEN OEIICNIFICAIION ILOU TANK
IXTCEN OEIICNIFICAIION WASHER VENI
MSHER, HOOD VENT

Mim«»£{iS

SSSSSSS£SSSS£

C-43
-------
C-44
-------
                                                en
                                                C/5


                                               S

                                               T3
                                                0)

                                                O

                                                Q.




                                                O

                                               to
                                               m

                                               Q


                                               X
                                                c
                                               _o

                                                ra
                                                o
                                                O)
                                                en

                                               JL
                                                3
                                               Q_


                                               r*^



                                                o


                                                en
C-45
-------
              77
              $ S
a   •uN9
23  38 8 1 - .  -3"8
 . .  .-85882*1
288.-..S2SS  .
                                   -° •"
                                  •  **
                                   82
5 ••<*
  ••<* k. u u. M f
 ..222S.
                 § s
                 u <


. s     s      sis!
si.   is      s  ° s
• •Q •   «      w  • H-
9 e M M u      cwwi
  OMCMjrf    £  ••   **
••- u •*^»s**°Q*-aF c
.i , j ? S 2  £  1  5 1 $
•;55^sst>u*2-a
* A a 6 u f  .  .  . -/ 8
 .  -  -•=S£822*I
225.-..222S  .
222iS£8S8i2
MMMWUJVQQO   «
S S Jt S 5-S  i  8-i-S-g
-— -^ •— c < •  >  >  > U* •
oaoM33uiuiufSa
 rWh.h.N.-K.N.KfvKK.fW
                                                           I
                                                      C-46
-------
C-47
-------
i s
• *
I 9 ! »«*^
  8



||.


* " 5
                                               :1
                                          iu   •* u
                                 222S22222S252
                                              C-48
-------
o r\ — —
     X g
     s ~
         ggg$-
           gg
          »i


         jl!
         I *" -

?i?ii;s;*n!*
:z;»»JS!.-.-.-=i
i « I .• «• .'-sio-g*
III||I|5|||S|

sis!!iii!!!ii
U £ U


?31


bl
•»••

vont


S/SCIIEE

wtk
                           C-49
-------
                         APPENDIX C.2
                 BLEACHING MODEL PROCESS UNITS

     This appendix presents emission points, emission factors,
and vent and wastewater stream characteristics for each of the
12 bleaching model process units (MPU's) presented in
Chapter 4.0.  The MPU's are defined based on wood type,
bleaching sequence, and percent chlorine dioxide substitution
level (see following summary table).  The following figures
(B1-B12) represent the emission points associated with each
model process.  Tables following each figure identify the
emission points within the model and the associated emission
factors and process vent and wastewater stream characteristics
of each emission point in the MPU.  These characteristics
include:
     •    Flow rate factor; and
     •    Hazardous air pollutant concentration.
     The assumptions and derivation of the emission factors
are presented in Appendix B.
     The following example presents how a model process unit
would be assigned  (or "mapped") to the bleaching process at a
pulp mill.  Assume the same mill in Appendix C.I has two
bleaching lines, one dedicated to bleaching hardwood
(1000 tons per day), the other bleaching softwood (1000 tons
per day).  The hardwood line uses a CdEHD process with 30%
chlorine dioxide substitution.  Because hypochlorite use has
been determined to result in increased chloroform generation,
the existence of a hypochlorite stage was designated a higher
criterion in model assignment than chlorine dioxide
                           C-50
-------
substitution.  Therefore, using the bleaching model summary
table as a guide, the Bl model process unit representing
hardwood pulp and hypochlorite use is assigned.
     The second bleaching line utilizes a OCdEDDED with 60%
chlorine dioxide substitution.  First, since the oxygen
delignification stage was assigned as part of the Kraft
softwood continuous model (P12) in Appendix C.i, the O stage
is not a factor in the model assignment.  Second, the model
process units represent the emissions from a process line, so
inexact matches are possible; however, the models incorporate
the elements that most significantly influence emissions.
Therefore, using the summary table as a guide, this sequence
would be assigned the softwod CdEDED (High) model (B8).
Definition of terms and references are presented in
Appendix C.3.
     The emissions from either process may then be estimated
using the appropriate figures and tables.  For example, the
chloroform emissions from the hardwood hypochlorite washer
would be estimated using the following steps:
     1.   Identify emission point code (EP__CODE) :  for model
          Bl, the hypochlorite stage washer is 151;
     2.   Identify the associated emission point emission
          factor ("Compound"_EF):  for chloroform (CHCL3_EP),
          the factor is 0.04 kg/Mg pulp;
     3.   Multiply factor by process line capacity:

  0.04 kg chloroform   1000 Ton pulp     1 Mg  _  36.4 kg chloroform
       Mg Pulp              Day        1.1 Ton           Day

     4.   Convert to annual emissions, assuming mill operates
          350 days per year:

       36.4 kg chloroform   350 Day = 12,700 kg chloroform
             Day           Year             Year
                            C-51
-------
        SUMMARY TABLE OF BLEACHING MODEL PROCESS UNITS


  Model process       Bleaching sequence
      unit          (% C102 substitution)3        Wood type
B-l
B-2
B-3
B-4
B-5
B-6
B-7
B-8
B-9
B-10
B-ll
B-12
CEHD (0%)
CEHD (0%)
CEDED (0%)
CEDED (0%)
CdEDED (low)b
CdEDED (low)b
CdEDED (high)c
CdEDED (high)0
CdEDED (100%)
CdEDED (100%)
O-Ed
0-Ed
Hard
Soft
Hard
Soft
Hard
Soft
Hard
Soft
Hard
Soft
Hard
Soft
a Key:    C    = Chlorine
          Cd   = Chlorine dioxide substituted for chlorine
          D    = Chlorine dioxide
          E    = Extraction
          O    = Oxygen/Ozone
  A low substitution range is 10 to 50 percent substitution.
  Less than 10 percent is considered to have the same
  emissions as 0 percent substitution.
c A high substitution range is 50 to 90 percent substitution.
  Greater than 90 percent is considered to have the same
  emissions as 100 percent substitution.
d An oxygen delignification precedes this sequence and is part
  of the associated pulping model for the process.
                          C-52
-------
                                 ft w
                                 h
                                            Q
                                            I
                                            LJJ
                                            O
                                             I
                                            c
                                            o

                                            1
                                            o
                                            03
                                            0)
                                            O)
C-53
-------
  h—i	
  ! 3 I  -  o

  i 21  i  i
  I IX :  —  <»
HCHUJE
u lu I xiwzujacz
_ i y ! "«!"«»'"'
                     > > >
I i 2
   i i ^ s i
          S

      >  > u
         UM
         V-------
5
rw
§











>
!
&
Si
S
m
M
•
Ui
i.
5
1














tte
"i
S
IU
§
o

^


5
i
1
i
i
uu
I
I1
1
a,
KN.UENE
^
1
2
i
kM
g
S
f





I

*
ua
§
1

r««.(S|«.^*>»f<4(M-------

(?) ^ 	 /7=
o1 v^C



f?^ ^. 	
i*-./ •*

• 	 1
T
(ffN 	 	 /r1
<5/ vjL.



fe^i ^ 	 T 	
I **! *




©/^F
^.. ...... .....i /



^"N ^. 	 	 	




T
©x*^3I

V Vfc*


0) * 	 : 	
W

1 (WW.....
s W
; "
i ,


*n
&£

^^
r<& j-» —

	 »



LU DC
o j±!
Z«R

-^
/^N— 	
._ \~)

— 	 —
j

UJ OC
u%$
§1

^^^
1 ^ 1
v /

N 	 »
x>
;

HI QT
CD yj
Otf «
s
CO P


d z
CO H

1






< z
CO 1-

1



1



^ i
UJ <
CO P





.



d =^
< z
UJ <
CO P















^

I
UJ

1
0
(**) ^
£ %
3 %*z -
rf 1- O ifl O)
s 5 y y c
O $ P 2 •—
	 , 	 »• $ Rp £
^ P UJ
-------
08/12/9]




i S
*
Ul
2
§
£
i_
g
$
1 "
r
o
5
ru
a» <
U i **•
C 0
i 5
S ; a.
<0 •-
.C
<-J i u
S «
4i O
i u
CW Wl
CD O
a.
1
*
*~
s
s







s
I ^
1 w
^
i






i


* *
". T

It


I
i ^- o
i i

«
S S %8%»!i%8!ii8!ii8
~ ~ «-«;«-«;«--;-
-$-$ 	 	
£Z>2>>>>>>8;>$>

;

»
§§§s§s§isss§ls

uuuuuuv^uuuuuou
_«_i^-J«J_*_i^-JJ_J^_4^

ll.iilulll
§4( tlJ^XMtfluiM
X"****>C O * VO 441'^'^
I - * .-g.ssssss^^
iiiiiitfitllti
i ,.«.Sot;s?^"?j;j;3s

? ? ? ? ? ? ? ? ? ? ? ? ? ?
11I1IIIII1!!!!

•^•O<^4^4^OO'V'4>
ftl«*^^^^O>^«— rg ^ ^t



















>•
I
i
S
2
Vi.
•f
M
!•

Si
*

















ICP245EF

MCHCll
UJ
i
tw


w
u
J
X

Ltf


J
W.
S'

5,


™i
*
u

S

™i

u
«







5
•*
^
i'
i
s '

3 S 5? S oi^o'S^mo*>aS
mr>.^«in>n)Wpn.^N.^-
I : . | > . 2 ^ i
-u||-^'-|"'-|"i8
i55.-1*i§SlSS52
2 as; s S" 	 ^~ss
iHU$!f!!!t-i
•IMMOMM 	 MM

? ? ? ? ? if ft f f i f f
9i Hii il iilllllll

^.S^KSSJS22"'*

a3sassssaasas»
C-57
-------
s
  o

  o
  w

  ui
   I
  (A

  i
  %
  i
  a
  ui
  §'

i = ^
! B
s
s
§
M
M
'i
Ul
3

  | £gggg3£g«$ggg§







     • «?3*?iJIiJ^£"f
    i ? li 11.? ? ? y?tif

    ..s^ssss = "«S2

   -i 33333333333333
                                   C-58
-------
Q

X
Q
UJ
Q
HI
TJ
O
 CO
 o>
TJ
 o
 CO
 0)
CO
m
 3
 O)
-------

2
<
t/t
1
<
§,
x
M
S
u
t
a.
>
	
u
<
o1
M.
w*
3
o'
£
ft
UJ
|


+ *
U hU
•0 rg
^- tr>

•«i/^fu->r^i/t«}O'O*-^(N^i/tio

il
— <>

* ~ *****!§** ~ §9 S 5

ss 	
ss», ,»*„„»*„,„„»„
tu
(J
Z
w
a.
-, ssssssssssssssss's
8 5S5SS5S55S255S55S
^
a.
J
a.
w
w
IU
§,
&
ttl
1'

uuuuuuuuuuuuu^u^u

! - s ^ . - ^
S SS»|!^| g 6
« *->u,i**uiil-*-c>*-c>
iu?£-i^-si-S^SS«Slt
JS>>il!S2SS>,.2"*2
MOt-*' btlU«
-O «£ — MMMMMMX'uvS'S*
- •XM«ooaoooo««o««
iK&s||f|?|||i||f
*.w 	 	
< — • • »#•*•!" ^»-.— fM rx «M IM rg to^e«aE

O^:5^*.^£^§^

^^MmmmNr wi •* ^*
i^ 2^
ftl -« M •- »M •-

*g S2S^*2S*^^


. «
»sx»S3(»s»aa!s *•>
iliiiiiiiiifhfii
Sg»,.2"!"-5«uS-.S-
|- 1| :ili8§|il! | ss
tHiillfifllffllf
• Sw-sfffrrrr!*????
* "* * t» * ^"•"^'"•••"^^'^''^rt'«'

? f ? f ? ? i t ? ? ? i i i i ? ?
H 1 1! il 1 1 X iS i! i X 8 2 2 i! ii

_ . »rt^,o>>»-«rf%N*OB
s;;5efc5S$ = = = 22sssi
mMininnmMmininmMMininMot

C-60
-------
  s 3i ;* nil K s s a « * * * !« s; K i
  oS««^«^«*'>;~<«O'»Minf>j
                S = r
8SS8SSS5SB3S853SS
                                                        C-61
-------
                                       o  2
                                       I!
                                              Q
                                              LU
                                              Q
                                              LU
                                              •O
                                              O
                                               I

                                              .o

                                              "3
                                              o
                                              CD
                                              jl)
                                              CO
                                              0)
C-62
-------
                                    i*
                                    u
                                    I
   § ; 77
   u
         rg^-«Njfsj~i^r\*^ojoi^-f>jf>*»-rv
  i °
  I £
s

5
   ~,  <<<<<<<<<

   £ : ssSssssiss
252
ZZi
                 =
                 S
      M O « M Wl i
               ? ? f ? ? ? ? ? ? ?
  I	L.
                                         •   »*
                                       ss
                                       •o **
                                       i;
                  «i!ii!i  j
                  >u«  u«i   w C
                    i 1 : i 1 : ! > 1
                  8 — I » *- a w  w **
              t f  ? ? ? ?
rv N N
o o o

? f f
                                            C-63
-------
I








   \




  ='

  I
  M.

  ut


  £i
  |



  I'




I i
O
5
S s
  O  *f 
-------
"In>

 2) -
          — ^ — — _
 8) —
C3



CO
                          UJ
                          o
                          til
                        - O

                       °S
                          //
                         / /
                         / /
                        / /
                       '  i
                                           i   /  /
                                             /    /
                                            /     /
                                          (&/





                                          §/
21

P
00
                                                                     ft  WJ


                                                                     II
                                                   Q
                                                   LLJ
                                                   Q
                                                   LU
                                                   T3
                                                   O



                                                   g


                                                   "s
                                                                             0)
                                                    O

                                                    CO
                                                    03
                                                                             CD
                                                    O)
                                 C-65
-------
«S
(Nl
3



$ 1
<
2 ;
• B ^ -
U * *
a. . fvj Jo
• g ^ -

" — 	 ._ . — — ... ... _)
ij -r^«-rj«;-i>;-«<«*--
: *
i «- O
! * +
; ' i^

;
, ' a'sjo'o'SJo'o'SSo'Kio'o'sis
L J.
l_ -p
'Sf£>$>$$$>$>>$>^:^$

1 \u
s ' 1
— U
41 X ,
t
, 03|||«««g|.|.«««|
1
% ' sxxzxzxxxsxxzxxxx

! i s
i s!H?!i i s
i ^* c £ ^ o «4*o«Sc>*S« >^
ijC>c-a«-5<«> * > 9
«5>« i_ — u *^
•2 T 1 1 a J i 1 J i J 1 f j 1 1 :
•1»s-l!l!!!!!!HI
, "SSSS""""?'!*^^^^?^
i 1 	
! ! ?????????????????

[ "•*
8
' U
















1




i
*













(CP24SEF
i
w
1
w
3'
•,

•A
s
UJ
w


1
-— •-
i'
-
*

w
i

-'
*
IW
(J

I1
s
£
S






Ul
U
1
w
!
^*
S . '
-* ^» -o *'*?'?
•i •> ^ — — (si



o'o'SJesfsssassJSWgKJft!;*

li*I*^^i$g*S^a


SSS««IS8lll3II«dl
Iff ^ •» If t
o> S C ^ o ^
•o 2S o A S u>

S^ S§3 = ^!S;§sSSc




sssssssssisssiggi

•+ •* -o
f^ « 
-------
 jj! «!S


              ggs
§§
iUiiilillfllllff
? ? ? ? f ? f ? ? ? ? ? ? ? ? y ?
SSSSS8SSSS88S8SSS
                          C-67
-------
                              ii
                              li
                                    Q


                                    CO
                                    Q
                                    LU
                                    Q
                                    LU


                                    O


                                    c
                                    .g

                                    to
                                    cu
                                    •o
                                    o
                                    ca
                                    jj>

                                    m

                                    co
                                    m
                                    3

                                    O)
C-68
-------
                         *

                         g
                         *
                                                s a! *
                                                if\ WS O
                             i
    !
    '
  -55
i
I «
      = 5 = 33 =
      <<<<<«<<«<<«<«
           C 4* •* C £ •*

          - S » i I * i   S

          g . fe " u S "  -I  -
• 2 - | * ; J J J J J J 11 : i I :
 w *- 5 « «»^. — *-s- — ****j « •• a M




I !f— f**^J-^^^^f^f^ojr%irij«Ni



 ? ? 111111.?".! I.?.? 11.? 1

                                              s
                               f  ? f ? ? ? ? 1 1 i t s ? t ? ?

                               lilillllillll!!!!
                                   C-69
-------
I
s
       !swWg3je»SSKj»jj*J»*j
  p  "

  x  XS3S8iogMin(%*gJ**j;*

  tu
  I
  i
  hi
  U|
  J
  i


  3
  H»
  U«
  §'
  w

  i
s
  ^-
  5





  ft'!

      I    |S!?S!
      i   i!j-!j-..j  -i


     ji||||||f|||f||||

     ? ? f ? ? f ? p ? ? ? ? ? p f f f
     Illlllllllllil]!!



  I
                                C-70
-------
                                  X w

                                  i!
                                          Q


                                          X

                                          x"
                                         Q
                                         LU
                                         Q
                                         LU
                                         •o
                                         O


                                         .o

                                         to
                                         o
                                         2

                                         O)
                                         ^c


                                         o
                                         CO
                                         _0)

                                         CD
                                         CD

                                         CD

                                         5
C-71
-------
 ' 5
 I	'r
    !!S5SSS5SSS£SSSSS
    Sjgggggg.^ggggggggg
    VI W»
 ! " i
CO k_	-4- -
    oooo
            oaoa
 i   J:1>!1  i
i.iil|:!!:!!l!i
                 ? S 2 5 S


                             CM ft* IO    
-------
»
f*t


i
       « — .0 «> —
    i^iiifflltffflf}!
                   1 1
                             C-73
-------
                          ill
                                      Q


                                      CO


                                      O

                                      X,

                                      Q
                                      HI
                                      Q
                                      UJ
                                      •o
                                      O
                                      co
                                      o
                                      O)
                                      O)
                                      c

                                      o
                                      CO
                                      jOJ
                                      CD

                                      CO
                                      CO
                                       O)
                                      IT
C-74
-------




V) ,
3
< '

«
3 ' - -
u ; * *
1 , LU LU

wi , Ln w



_ o
- >

| iiiilUWUJUUJjULUlUUJlilUJ


J
u QcarujLULU£UjLuvu£jwLULULugiLUM
3 "* *"
LU
i
a.
|' , a s s s a s 9 3 S S 8 S 9 s § I i
LU !
£ XXXXXXZXXXXXXXXXZ
«— UUUUUUUUUUUUUUUJJU
1 <<<<<<<<<<<<<<<<<

— C «i -* C 6 .*
- S * £ * * S
 > 8 > • M w
^Mb«C OA)4lO44tCv^Cw^
4j£CV-4*' Xv***Bi»C>5<* > 5
*£ : i f f I f ||*||: s|:
ril'^sassss •&$;&&&&
5Sw5o>«««««««»««*«
«^r?riiiiii^^^^^^
? ? ? ? ? ? ? ? ? ? ? ? ? ? ? ? ?
i llllillillillHul

| 35 33 S3 3 S SS 3 5 SSg S2
a1
UJ
§
|' SS55SSSSSSSSS55SS
















X
I
1

0
s
s
vt
(A
'«
LU
00
1
X












LU
s
HCNCL3EF
LU
i
i
-
M'
u
X

J
u


1
u

w
M.
n


***!


*l

5
u

s'
y

LU
<



IS

§
III
1
g




UJWWWWWUUJUJWUIUJJUWU1UIW
$$8» S > S *- *-
*- u ^ u *• C C
£ fc ^ — ^ * — - > *->
iiiiillllljllj|i|
? ? ?" i t ? ? j g ? g" g" g" g" g* g' g"
if 8 ii H i! 2 i H i :i 1 1 1 2

•»«3aaSSSSS5!S5SS2!:i

85SSSSS3S55SSS853
C-75
-------
§ -
    »IWtMW
    tnr4*--
  "T"


 "II"
  1AJ
  I

  a
z

s
        -   i
        'tlh
    ? ?
   imiimiiiiiin
   • SmZmmSmZZmmmmmmZ
               S3
                        C-76
-------
                                  * «

                                  ll
                                         Q


                                         X
                                         O
                                         o
                                         Q
                                         LJJ
                                         Q
                                         111
                                         T3
                                         O
                                         o
                                         C
                                         CD
                                         3
                                         0)
                                         O)
                                         CD

                                         CD

                                         3
                                         O)
C-77
-------
  il
   s
        M*«*0f>m
Z U-
        M^pgrg^(%((V*-(M(M.-(MfNt^-'^
     55
•8 ' 2
5 i
             o
       1 1 1 1 1 1 1 1 1 1
                    «., u U O Jj O
    i     — •{^^••••^^^••^ovveati
    1  u*- 5 *«»*-——•— w — *^ii«*'i«

      i^iiif Hff ft!!!!!
            f«»^>^wv(M)%j(Mrg(Mi
11 ? I.?.? 1.? 111.

VWV«*W*Vb«*
                                   g ; S * ;! 3 $ 3 3 3 1 3 3 £
                                              rg fs» •* rw 
-------
S -

    "1--
        — -0.0.-
  ....



  *
   '
    ?????????????????
    Illllllllllllllll
                               C-79
-------
-	Co
                                                    Q
                                                    LLJ
                                                    Q
                                                    LU
                                                    T3
                                                    O


                                                    O

                                                    1
                                                    I
                                                    O)
                                                    .92
                                                    CO

                                                    o
                                                    m

                                                    I
                                                    o>
                     C-80
-------
    o tn
 3i
 u

 li

 2
i	(-

; 3
    !!s;;ss;;s;ssssss
| . 2

                           S

                           S
                           ¥
                           .—f_.
                               *$*
                             VMtM

                             II
       «i — oooooo J *» ^ i (# "3
      . IM«^ — — *-«-^-5a*3«*
                             lilh
               MWMWWlAMM
             o o a o o
     ? ? ???'??? ? ? ? s ? ? ?' ? ?
                            M O » VI M	
                            uuuuuujuiujaoaoaaujujw

                            t ? i t i i i i t f ? ? f ? ? f ?

                            Illllllllllllllll
                             •S Sg-S 8 s ass 3 5S-125
                             naTknm9,,9O>^*wvM^^^^^mp^P't
     222S2ooooeoooooo°
     ••••••••••••••••S
                            «oooooooooooooooo
                                C-81
-------
3
     -a -o -a — ««••
     II???????????????
     ii1liiii!l!lii!!l
     2222222°222222222
                                C-82
-------
EOF TOWER VENT
02 DELIGNIFICATION

    BLOW TANK
                                      o
                                      o

                                      "O

                                      CO
                                      a.
                                      O
                                      LLJ

                                      6
                                      i
                                      a*
O
CO
_a)

CD

CD
0)

ul

0
                                      _

                                      6
1
                                      QQ


                                      1
                                      O)
                                      il
        C-83
-------










2
t
*
3
U
s
ul
*
o1
M
U
Q!
~J
>
1
U
1
UJ
1
U
UJ
a.
i

J


I
UJ
,
Ul
i
i1














PVJ iv rg KI «-
SS3S3
— - - - *



i i i i •'
S S •* -r 0
~ — ~ - <"

> S» > S! S>





|| || S

S | 5 S S
UJ UJ UJ UJ UJ
* UJ
S s * 2
SS . S S
S « i « 5
«J -J
S S  *» |>
S 5 S S I


*****























Factor
g
1
2
"Z
i
X











•ft.
S!
«
5
i
£
2
UJ
^
m
£
N
S
"i
"'
H

U
HJ
M'
.J
U

1
UJ
s*
*

lit


«'
S
M
UJ
U

w.
??'

u>
i


1
8
S
8
l'


















? ? r ? •?
*- » o -o m
•*•"-»««"




sigsa




3§£$3
* h. - ^ <0
(>J K> f>t
t—
UJ > »—
* S « S
-1*3!
a »- OK iu
2 S 1 2 S
ggaaa
• a a f f f
»- •»> Wl N- 9-
o o o o 5












































Ul
w
3
i
s
H-
£
s
•-
«k
1
U.
i
3

ACETOPHNE
"l
8

§'
U.
U
1
i

S1
s
s
55
i

!•>
«
Ul
8
s
i'


i
i
s'
8
i1


- - 1M - -
JN o to ^ «*
•* — sr o S
IM ^ (« — —
£2csS
- ~ ~ - -
















???
8 » 2
•0 - 0
«r (M w> -* «
§££!§
•* *- o> ** •-

f^ Q t/> O O
'O S « fn •-


» S
S5. S
S S! 3 *
S 5 « - S
2 « % « 5
uj S w «j
g s a a a
a a * " ?
|| %%%
S 3 S o S



C-84
-------
                                     O
                                     O
 EOP TOWER VENT
02 DELJGNIFICATION
    BLOW TANK
                                     o
                                    CO,
                                    Q_
                                    O
                                    LLJ
                                    6
                                     O)
O
CO
5
o
£
0
                                    6
3
i2
cvi
5
I
O)
IT
        C-85
-------
S










U)
D
1
z
g
u
X
in
gi


o1
S
1
_j
>
&
*"l
SOURCE
UI
UI
&.
1
„
=
2

!
UJ
8
i'















rv IM  O K» -O



iilii



i^**s
^ ^ ^ « in
10 (NJ m fM f%J
~ * + « XI
O o <-•-•>-
S S S 3 3
UJ UJ 5 S W
s ; s s s
O O uj ui uj
^ S S S °
•* •* -* ** HT
IV N AJ N N





































S
u.
s
£


U
I

1
5

ACETOPHNE
-i
s,
8

I
^
i
§

u.
I
Ik
i
u.
UJ
<
u>
if

!
UJ
!


— *- N ^ i-
^ <* « AJ ^
fM ^ »>J »- »»
O •* 3 -O O
trt INJ *M ^ **

















ils
•o -a ~
ni in m -»
!S!?
« >» « «
^a§^



|2 « S 5
S . | s ^
8 g - * *
^ _i
::III
a 5 T T T
^ ^ & i &
Sa 8 8 S
O UJ UJ IM
S S |.S 2
*v rtj oi M ey
                                    C-86
-------
   APPENDIX C.3




DEFINITION OF TERMS
Abbreviation
ACET EF
MEOH EF
CTET EF
MEK EF
H2S EF
MMER EF
DIMES EF
DIMDS EF
ALPINE EF
HCL EF
CL2 EF
CL02 EF
MECL EF
CHCL3 EF
L_BENZ_EF
PHENOL EF
TCDD EF
TCDF EF
MCHCL3 EF
TCP245 EF
TCP246 EF
Description/Compound
Acetone
Methanol
Carbon tetrachloride
2-Butanone (Methyl ethyl ketone)
Hydrogen sulflde
Methyl mercaptan
Dimethyl sulfide
Dimethyl dfsulfide
Alpha-plnene
Hydrogen chloride
Chlorine
Chlorine dioxide
Methylene chloride
Chloroform
Benzene
Phenol
2.3,7,8-Tetrachloro-p-dioxin
2,3. 7,8-Tetrachloro-p-furan
Methyl chloroform (1,1,1 Trichloroethane)
2,4,5-Trichlorophenol
2,4,6-Trichlorophenol
Units3
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
       C-87
-------
DEFINITION OF TERMS (Continued)
Abbreviation
CLPHEN EF
POP EF
B PINE EF
ATERP EF
ACROLEIN EF
ACETAL EF
PROPAL EF
DACETON EF
TOLUENE EF
HEXANE EF
CMETHANE EF
PCYMENE EF
PCDB EF
FORM EF
ACETOPHN EF
DIMTS EF
CARBDIS EF
THC EF
TOTHAP EF
TOTVOC EF
TRS EF
MPU CODE
PROC TYP
PULPJYP
WOOD TYP
EP CODE
SOURCE
Description/Compound
Chlorophenolics
Pentachlorophenol
Beta-pinene
Alpha-terpene
Acrolein •
Acetaldehyde
Propionaldehyde
Dichloroacetonitrile
Toluene
Hexane
Chloromethane
p-Cymene
1 ,4-Dichlorobenzene
Formaldehyde
Acetophenone
Dimethyl trisulfide
Carbon disulfide
Total hydrocarbon
Total HAP
Total VOC
Total reduced sulfur
MPU code
Process type
Pulp type
Wood type
Emission point ID
Source description
Units3
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
kg/Mg pulp
Unitless
Unitless
Unitless
Unitless
Unitless
Unitless
             C-88
-------
                      DEFINITION OF TERMS (Continued)
Abbreviation
VFLOW/AC
SFLO_FAC
VHAP CON
SHAP CON
HWD
HAL STATUS
SWD
C
Cd
E
H
D
ENCLOSURE
Description/Compound
Vent flowrate
Wastewater stream flowrate
Vent HAP concentration
Wastewater stream HAP concentration
Hardwood
Is the vent stream halogenated (yes or no)
Softwood
Chlorine
Chlorine dioxide substitution
Extraction
Hypochlortte
Chlorine dioxide
Number of enclosures required
Units3
scmm/Mg
pulp/day
je/min/Mg
pulp/day
ppmv
mg/L
Unitless
Unitless
Unitless
Unitless
Unitless
Unitless
Unitless
Unitless
Unitless
kg/Mg pulp = Kilograms of air emissions per megagram of pulp produced.



scmm/Mg pulp = Standard cubic meters per minute vent flow per megagram of pulp produced.



I/mm = Liters of wastewater per minute.



ppmv =  Parts per million by volume.



mg/je =  Milligrams of compound(s) per liter of wastewater.
                                   (J-89
-------
REFERENCES
1.   Memorandum from Olsen, T.R., Radian Corporation, to
     Shedd, S.A., EPA/CPB.  Revised model process units for
     the Pulp and Paper NESHAP.  September 21, 1993.
-------
TECHNICAL REPORT DATA
(Please read Instructions on the reverse be fan completing)
REPORT NO. 2.
EPA-453/R-93-0503
TITLE AND SUBTITLE
Pulp, Paper, and Paperboard Industry - Background
Information for Proposed Air Emission Standards
Manufacturing Processes at Kraft, Sulfite, Soda and Semi-<
AUTHOR(S)
PERFORMING ORGANIZATION NAME AND ADDRESS
Office of Air Quality Planning and Standards
US Environmental Protection Agency
Research Triangle Park, North Carolina 27711
. SPONSORING AGENCY NAME AND ADDRESS
Office of Air and Radiation
US Environmental Protection Agency
Washington, D.C. 20460
3. RECIPIENT'S ACCESSION NO.
S. REPORT DATE
October 1993
6. PERFORMING ORGANIZATION CODE
Ihemical Mills
8. PERFORMING ORGANIZATION REPORT NO.
10. PROGRAM ELEMENT NO.
11. CONTRACT/GRANT NO.
68-D1-0117
13. TYPE OF REPORT AND PERIOD COVERED
Interium Final'
14. SPONSORING AGENCY CODE
EPA/200/04
. SUPPLEMENTARY NOTES
ABSTRACT


  National emission standards  for hazardous air pollutants  (NESHAP)
  are being proposed for the pulp and paper industry under authority
  of Section  112 (d) of the Clean Air Act as amended in 1990.  This
  background information document provides technical information and
  analyses used in the development  of the proposed pulp and paper
  NESHAP.   This  document  covers air emission  controls  for wood
  pulping and bleaching processes at pulp mills and integrated mills
  (i.e.,  mills that  combine  on-site  production, of both  pulp and
  paper).  Effluent guideline limitations for  pulp and paper mills
  are  being  developed  concurrently  under the  Clean Water  Act.
  Technical  information   used  for   the  development  of  effluent
  guideline limitations is in  separate documents.
KEY WORDS AND DOCUMENT ANALYSIS
DESCRIPTORS
ir Pollution
jlatile Organic Compounds
.zardous Air Pollutants
alp and Paper Mills
Up Mills
per Mills
IISTRIBUTION STATEMENT
limited
b.lDENTIFIERS/OPEN ENDED TERMS
Air. Pollution Control
19. SECURITY CLASS (This Report)
Unclassified
20. SECURITY CLASS { Tit is page >
Unclassified
c. COSATI Field/Group
13 b
21. NO. OF PAGES
385
22. PRICE
 Form 2220-1 (R«». 4-77)   PREVIOUS EDITION is OBSOLETE
-------