AQ_F_1900002_20140618_EI_Cmb-EI-File

2013 Emissions Inventory Review / Data Tracking Form
Facility Name: Performance Fibers, Inc... Facility ID: 1900002
Facility Assigned to: Data Entry: Chatham County
Classification: David Miller Confidential Copy Submitted?
Title 0 YES
JR NO
Initial Review/Data Entry
I Enter date received into ED. Date Received:
Ef- Assigned to appropriate individual. Date Assigned: Date Due:
45 Paper copy submitted: One copy received with supporting documentation,certification form signed by responsible official,and
appears generally complete;OR
Electronic copy submitted: All supporting documentation and certification form(with time/date stamp)signed by responsible
official has been received.
Comments: Over all there was a drop of about 14%in emission,which the Company accredit this to 15%decrease in fuel use.
The exceptions are:Biphenyl: increase use of specific chemicals;Acctaldehyde: increase use of specific chemicals;
ou,ling in the use.
Inventory Review
! All forms and supporting documentation appear to be complete if paper submission(check ED OS data if electronic).
[7j Contact,address,phone number changes entered into I-Beam/Facilities if necessary.
Ef All known operating scenarios,control devices,and emission release points have been entered for each emission source(permitted,
insignificant,and unpermitted)or note that the emission source was not operated or.not required to report.
ET Evaluate"U" sources for significance and address according to policy.
E!r Calculations/forms appear to add up correctly.
Z All compliance issues are being addressed(e.g.Toxics limits,above TV thresholds,large emissions increase/decrease,installation
without a permit).
Q All volatile HAPs/TAPS were included in the VOC total.
p Calculations and control efficiencies appear correct. Emission factors are the best available and most current factors appropriate
for the reporting facility(e.g. stack testing,AP-42,etc.).
p Review facility comments and address any issues.
ET Update ED(Data Entry Main)if additional information is required(corrections due date and date received).
a Check all ED QA/QC reports.
p Comparison with previous emission inventory must be made and outliers(> 10%)must be investigated and explained.
Cr Put inventory review comments and summarize any changes in ED-Data Entry Main"DAQ internal comments".
C� Print and attach the facility total report.
Date Review Complete: Signature:
Date Submitted to EI Coordinator:
Date Approved: / j 4 Initials: lid

Facility Total CY 2013 Emission Summary Recorded in ED Facility ID #: 1900002
Facility Name: Performance Fibers, Inc. Permit#(s): 02657T29
Hazardous Air Pollutants Actual Emissions
(HAPs) (Pounds/Year)
Po11jft0A/or Toxic Air Pollutants CAS CY 2013 CY 2012 Demini- % `
(TAPS) from ED from Fees mus Change
Toluene 108-88-3 12.74 12.97 100.0 -1.8%
Vinyl acetate 108-05-4 2.62 2.06 100.0 127.2%
Xylene (mixed isomers) 1330-20-7 2.23 2.20 100.0 1.0%
Largest Individual HAP Ethylene glycol 245,723.50
lbs
Total HAP Emissions 253,460.36
lbs
DAO's Comments Regarding Inventory
Over all there was a drop of about 14%in emission,which the Company accredit this to 15%decrease in fuel use. The
exceptions are:Biphenyl: increase use of specific chemicals;Acctaldehyde: increase use of specific chemicals;HCFC-22:
doubling in the use.
09/04/2014 Page 4 of 4

Facility Total CY 2013 Emission Summary Recorded in ED Facility ID#: 1900002 '
Facility Name: Performance Fibers, Inc. Permit#(s): 02657T29
Hazardous Air Pollutants Actual Emissions
(RAPS) (Pounds/Year)
Pot►j�U((or Toxic Air Pollutants CAS CY 2013 CY 2012 Demini- %
(TAPS) from ED from Fees mus Change
Polycyclic Organic Matter(Specific Compounds from OAQPS 4,583.61 596.74 1.0 668.1
or Tip
Biphenyl(Component of 833291POMTV) 92-52-4 4,583.30 596.38 10.0 1668.5%
Naphthalene (Component of 833291POMTV) 91-20-3 0.307730 0.358030 1.0 1-14.0%
Acetaldehyde 75-07-0 1,288.01 2,826.94 10.0 1-54.4%
Acetic acid 64-19-7 28.77 22.70 100.0 26.7%
Acrolein 107-02-8 0.009000 0.011000 10.0 -18.2%
Benzene 71-43-2 8.91 9.01 1.0 -1.1%
Butadiene, 1,3- 106-99-0 0.004000 0.005000 1.0 -20.0%
CFC- 113 (1,1,2-trichloro-1,2,2-trifluoroethane) 76-13-1 10.74, 3.07 100.0 249.8%
Cumene 98-82-8 0.580000 0.580000 100.0 0.0%
Dichlorobenzene(p), 1,4- 106-46-7 0.567870 0.664440 1.0 -14.5%
Dioxane, 1,4- 123-91-1 80.84 80.92 0.01 -0.1%
Epoxybutane, 1,2- 106-88-7 2.05 1.83 1.0 112.0%
Ethyl benzene 100-41-4 0.580000 0.580000 100.0 0.0%
Ethylene glycol 107-21-1 245,723.50 234,461.52 100.0 4.8%
Fluorides (sum of all fluoride compounds as mass of B6984-48-8 0.023200 0.018100 10.0 128.2%
ion)
Formaldehyde 50-00-0 45.73 51.67 10.0 1-11.5%
HCFC-22 (Chlorodifluoromethane) 75-45-6 3.58 . 1.02 1251.0%
Hexane, n- 110-54-3 914.35 1,063.98 100.0 -14..1%
Methanol (methyl alcohol) 67-56-1 4.46 9.69 1,000.0 1-54.0%
Methyl chloroform 71-55-6 0.000150 0.000100 100.0 NIA
Polycyclic Organic Matter(Inc PAH, dioxins,etc.NQ30M 0.051200 0.059080 1.0 -13.3%
&AP 42 historic)
Selenium Compounds SEC 0.012800 0.014020 10.0 -8.7%
Styrene 100-42-5 0.100000 0.100000 100.0 0.0%
TCE(trichloroethylene) 79-01-6 386.55 498.02 1,000.0 1-22.4%
09/04/2014 Page 3 of 4

Facility Total CY 2013 Emission Summary Recorded in ED Facility ID#: 1900002
Facility Name: Performance Fibers, Inc. Permit#(s): 02657T29
Hazardous Air Pollutants Actual Emissions
(HAPs) (Pounds/Year)
Po11&0A(or Toxic Air Pollutants CAS CY 2013 CY 2012 Demini- %
(TAPS) from ED from Fees mus Change
Arsenic& Compounds(total mass of elemental AS, arsine and 0.096650 0.111270 0.01 -13.1%
all inorganic compounds)
Arsenic Unlisted Compounds-Specify Compound ASC-Other 0.096650 0.111270 0.01 43.1%
(Component of ASC)
Beryllium &compounds(Total mass) 0.005390 0.006310 1,0 -14.6%
Beryllium Metal (unreacted) (Component of BEC) 7440-41-7 0.005390 0.006310 1.0 1-14.6%
Cadmium & compounds(total mass includes elemental metal) 0.520000 0.608740 0.1 I-14.6%
Cadmium Metal, elemental, unreacted(Component 7440-43-9 0.520000 0.608740 0.1 -.14.6%
of CDC)
Chromium-All/Total(includes-Chromium(VI) categories, 0.663100 0.775200 0.1 -14.5%
metal and others)
Chromic acid(VI) (Component of SolCR6&CRC) 7738-94-5 0.663100 0.775200 0.01 1-14.5%
Chromium(VI)Soluble Chromate Compounds(Component of 0.663100 0.775200 0.01 -14.5%
CRC)
Chromic acid(VI) (Component of S61CR6&CRC) 7738-94-5 0.663100 0.775200 0.01 -14.5%
Cobalt& compounds 0.047290 0.049270 1.0 -4.0%
Cobalt Unlisted Compounds-Speck Compound COC-other 0.047290 0.049270 1.0 -4.0%
(Component of COC)
Lead&compounds 0.237460 0.277130 1.0 -14.3%
Lead Unlisted Compounds-Speck Compound PBC-Other 0.237460 0.277130 10.0 -14.3%
(Component of PBC)
Manganese& compounds 0.183550 0.211430 10.0' 1 -13.2%
Manganese Unlisted Compounds-Specify NINC-Other 0.183550 0.211430 10.0 -.13.2%
Compound(Component ofAMC)
Mercury & Compounds-all total mass includes Hg Vapor 0.122860 0.143620 0.001 1 -14.5%
Mercury, vapor(Component of HGC) 7439-97-6 0.122860 0.143620 0.001 1-14.5%
Nickel& Compounds,sum total mass includes elemental 1.10 1.20 1.0 -8.3%
Nickel metal(Component of NIC) 7440-02-0 1.10 1.20 1.0 -8.9%
09/04/2014 Page 2 of 4

Facility Total CY 2013 Emission Summary Recorded in ED Facility ID#: 1900002
Facility Name: Performance Fibers, Inc. Permit#(s): 02657T29
Green House Gases Pollutants (GHG) Actual Emissions
Tons/Yr
Pollutant CAS CY 2013 CY 2012 Demini- Change
from ED from mus
Hydrofluorocarbons(HFCs); 0.046000
BFC Not Not N/A
Reported Reported
HFC-134a (1,1,1,2-Tetrafluoroethane) 811972 0.046000 0.048000 0.05 -4.2%
Nitrous Oxide (N20) 10024972 0.500800 0.621000 1.0 -19.4%
Carbon Dioxide (CO2) 124389 28,410.28 33,239.48 5,000.0 -14.5%
Methane (CH4) 74-82-8 0.560800 0.631000 10.0
CO2 equivalent(sum of individual GHG pollutant emission 25,979.58 metric tons
times their 1995 IPCC Global Warming Potential(GWP),
converted to metric tons)
Criteria Pollutants Actual Emissions
(Tons/Year)
Pollutant CAS CY 2013 CY 2012 Demini- %
from ED from Fees mus Change
CO Co 19.95 23.34 0.5 -14.5%
NOx NOx 24.11 28.06 0.5 1-14.1%
PM(TSP) TSP 10.76 11.34 0.5 -5.1%
PM10 PM10 10.75 11.33 0.5 -5.1%
PM2.5 PM2.5 10.75 11.33 0.5 -5.1%
S02 S02 0.260000 0.290000 0.5 1-10.3%
VOC VoC 141.72 131.00 0.5 8.2%
Hazardous Air Pollutants Actual Emissions
(RAPS) (Pounds/Year)
Po1I&VI&/or Toxic Air Pollutants CAS CY 2013 CY 2012 Demini- %
(TAPS) from ED from Fees mus Change
Antimony & Compounds(total mass, inc elemental SB) 399.89 405.45 10.0 -1.4%
Antimony Unlisted Compounds-Specify Compound SBC-Other 399.89 405.45 10.0 -1.4%
(Component of SBC)
09/04/2014 J Page 1 of 4

R e-,,z vlz W
FACILITY WIDE EMISSIONS EXPLANATIONS
Absolute%
Difference
Carbon Monoxide(CO) 23.33 19.97 14.4 Approximately 15%decrease in fuel usage
(mostly natural gas)from 2012 to 2013
Nitrogen Oxides(NOx) 28.05 24.11 14 0 Approximately 15%decrease in fuel usage
(mostly natural gas)from 2012 to 2013
Total Particulate Matter(PM) 11.35 10.75 5.3
PM-10 11.35 10.75 5.3
PM-2.5 11.35 10.75 5.3
Sultur Dioxide(S02) 0.27 U.27 1.5
Total VOC/TOC(incl. HAP) 130.79 141.38 8.1
Absolute%
Difference
Approximately 15%decrease in fuel usage
Garton Dioxide(CO2) 33,238 28.414 14.8 (mostly natural gas)from 2012 to 2013
Methane (CH4) 0.64 0.54 14 5 Approximately 15%decrease in fuel usage
(mostly natural gas)from 2012 to 2013
Nitrous Oxide(N20) 0.81 0.52 14 5 Approximately 15%decrease in fuel usage
(mostly natural gas)from 2012 to 2013

I ,
otute
�ii'ference ��
Acetaldehyde 2,826.97 1,288,07 54A Decreased production hours,fuel usage
and specific chemical usage
Acetic Acid 22.70 28,77 26_7 Appuxirnate 20%increase in specific
chemical
Acrolein 0.01 0.02 22.3
Slight increase.in genefatur run time
Acrylic Acid 0.00 0.00 #VALUE!
Antimony Compounds 405.45 399.90 1.4
Arsenic Compounds 0.11 0.10 143 Approximately 15°'o decrease in fuel usage
� . (mostly natural gas)from 2012 to 2013
Benzene 9.04 8.91 1.5
Beryllium Compounds 0.01 0.01 14A Approximately 15%decrease in fuel usage
(mostly natural gas)from 2012 to 2013
Biphenyl 596.38 4,583.30 •5 Increased Dowtherm usage without
immediate recycle implemented
Butadiene, 1,3- 0.01 0.01 22.3
Slight increase in generator run time
Butylene Oxide, 1,2- 2.64 2.05 22A Approximate 20%decrease in specific
chemical
Cadmium Compounds 0.61 0.52 14 5 Approximately 15%decrease in fuel usage
(mostly natural gas)from 2012 to 2013
Chromium Compounds 0.78 0.66 14 5 Approximately 15%decrease in fuel usage
(mostly natural gas)from 2012 to 2013
Chromium VI 0,00 0.00 283 Approximately 15%decrease in fuel usage
(mostly natural gas)from 2012 to 2013
Cobalt Compounds 0.05 0.04 12,0 Approximately 15%decrease in fuel usage
(mostly natural gas)from 2012 to 2013
Cumene 0.58 0.58 0.0
Dichlorobenzene, 1,4- 0.66 0.57 145 Approximately 15%decrease in fuel usage
(mostly natural gas)from 2012 to 2013
Dioxane, 1.4- 80.91 80.84 0.1

ott'1Ference
Ethylbenzene 0.58 0.58 0.0
Ethylene Glycol 234,461.18 245,724.86 4.8
Fluorides 0.02 002 28.7 Approximately 15%decrease in fuel usage
(mostly natural gas)from 2012 to 2013
Formaldehyde 52.13 46.14 11.5 Approximately 15%decrease in fuel usage
(mostly natural gas)from 2012 to 2013
Hexane 1,064.00 914.40 14,1 Approximately 15%decraasP in fuel irsage
(mostly natural gas)from 2012 to 2013
Lead Compounds 0.28 0.24 14A Approximately 15%decrease in fuel usage
(mostly natural gas)from 2012 to 2013
Approximately 16%decrease in fuel usage
Manganese Compounds 0.21 0.18 14.2 (mostly natural gas)from 2012 to 2013
Mercury Compounds 0,14 0.12 14,5 Approximately 15%decrease in fuel usage
(mostly natural gas)from 2U12 to 2U13
Methanol 9.69 4.46 53.9 Approximate 50%decrease in specific
chemical
Naphthalene 0.36 0.32 12.7 Approximately 15%decrease in fuel usage
(mostly natural gas)from 2012 to 2013
Nickel Compounds 1.20 1.05 13,1 Approximately 15%decrease in fuel usage
(mostly natural gas)from 2012 to 2013
Polycyclic Organic Matter(POM) 0.06 0.06 6.3
Selenium Compounds 0.01 0.01 13 5 Approximately 15%decrease in fuel usage
(mostly natural gas)from 2012 to 2013
Styrene 0.10 0.10 0.0
2,2,4-Trimethylbenzene 3.95 3.95 0.0
Toluene 12.99 12.74 2.0
Trichloroethylene 498.02 380.55 22.4 Approximate 20%decrease in specific
chemical
Vinyl Acetate 2.06 2.62 26.7 Approximate 20%increase in specific
chemical
Xylenes 2.22 2.23 0.5

At"uto%
Diftemnee
Chlorodifluoromethane 1.02 3.58 250,0 Approximate 100%increase in specific
chemical usage
Dichlorodifluoromethane 0.00 0.00 #VALUE!
1,1-Dichloro-l-fluoroethane 0.00 0.00 #VALUE!
Mothyl chloroform 0.00 0.00 28.7 Approximate 100%increase in specific
chemical usage
1,1,1,2-Tetrafluoroethane 96.60 92.40 4.3
Trichlorofluoromethane 350.00 600.00 71.4 Approximate 100%increase in specific
chemical usage
Trichlorotrifluoroethane 3.07 10.74 2 ,p Approximate 100%increase in specific
chemical usage

Performance Fibers, Inc.
New Hill , North Carolina
CY2013 Point Source
Air Emission Inventory
Report
June 2014

Emission Source Emission Source Description Control Device ID Control Device
ID No. No. Description
IOV-1 Pyrolysis furnace(400,000 Btu per hour maximum heat N/A N/A
input rate)
IOV-2 Pyrolysis furnace(400,000 Btu per hour maximum heat N/A N/A
input rate)
IEG-1 Diesel-fired emergency generator (536 horsepowerN/A N/A
MACT ZZZZ maximum rated power output)
IEG-2 Propane-fired emergency generator (38 horsepower N/A N/A
MACT ZZZZ maximum rated power output)
IEG-3 Propane-fired emergency generator (78 horsepower N/A N/A
MACT ZZZZ maximum rated power output)
ICP-28 Diesel-fired emergency fire water pump(290 horsepower N/A N/A
MACT ZZZZ maximum rated power output)
CP-593 Diesel-fired emergency fire water pump(235 horsepower N/A N/A
MACT ZZZZ maximum rated power output)
IVT-I Esterification mix and feed tanks of various capacities N/A N/A
IHT-8 Diesel fuel tank(2,000 gallon capacity) N/A N/A
IHT-9 Propane fuel tank(30,000 gallon capacity) N/A N/A
IVT-14 No.6 fuel oil tank(30,000 gallon capacity) N/A N/A
IHT-15 Unleaded gasoline tank(900 gallon capacity) N/A N/A
IHT-18 Diesel fuel tank(900 gallon capacity) N/A N/A
IVT-19 Virgin ethylene glycol tank(200,000 gallon capacity) N/A N/A
IVT-20 Spent ethylene glycol tank(200,000 gallon capacity) N/A N/A
IHT-21 Unleaded gasoline tank(900 gallon capacity) N/A N/A
IHT-22 Diesel fuel tank(270 gallon capacity) N/A N/A
q IHT-23 Diesel fuel tank(270 gallon capacity) N/A N/A
•J
1 w IHT-25 Purified ethylene glycol tank(30,000 gallon capacity) N/A N/A
'O
IHT-28 Ethanolamine tank(11,420 gallon capacity) N/A N/A
IVT-30 No.6 fuel oil tank(30,000 gallon capacity) N/A N/A
IVT-31 Terephthalic acid silo(25,000 cubic feet capacity) N/A N/A
IVT-32 Terephthalic acid silo(25,000 cubic feet capacity) N/A N/A
IVT-33 Terephthalic acid silo(25,000 cubic feet capacity) N/A N/A
IVT-34 Virgin ethylene glycol tank(200,000 gallon capacity) N/A N/A
IVT-35 Treated finish tank(12,500 gallon capacity) N/A N/A
IVT-38 Treated finish tank(12,500 gallon capacity) N/A N/A
IVT-39 Treated finish tank(12,500 gallon capacity) N/A N/A
IVT40 Treated finish tank(12,500 gallon capacity) N/A N/A
IVT41 Untreated waste finish tank(12,500 gallon capacity) N/A N/A
IVT44 No. 6 fuel oil tank(60,000 gallon capacity) N/A N/A
a

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Emission Source Emission Source Description Control Device ID Control Device
ID No. No. Description
IVT45 No.6 fuel oil tank(235,000 gallon capacity) N/A N/A
IVT-78 Di-isopropyl amine tank(10,000 gallon capacity) N/A N/A
IVT-92 Waste oil tank(2,000 gallon capacity) N/A N/A
IVT-235 Caustic tank(12,000 gallon capacity) N/A N/A
WT-236 Caustic tank(12,000 gallon capacity) N/A N/A
IVT-237 Caustic tank(12,000 gallon capacity) N/A N/A
IVT-238 Caustic tank(12,000 gallon capacity) N/A N/A
IVT-239 Caustic tank(12,000 gallon capacity) N/A N/A
INT-I Nitrogen tank(11,000 gallon capacity) N/A N/A
IXT-506 Alan IV copolymer extruder MIST2 Condenser/mist
eliminator
IRG-1 Process chiller N/A N/A
- IRG-2 Process chiller N/A N/A
' - IRG-3 Process chiller N/A N/A
- IRG4 Process chiller N/A N/A
ITEGCU Triethylene glycol cleaning unit N/A N/A
�- IQCFMR Finish preparation(QC finish make-up room) N/A N/A
p -O 1 Alan III vessel APT-101 A draining vents N/A N/A
s'7 F-02 Alan IV vessel APT-101B draining vents N/A N/A
N` IF-03 Alan III vessel APT-117A flush dumping line N/A N/A
ZE o-
IF-04 Alan IV vessel APT-117B flush dumping line N/A N/A
ICA
Esterification vessel fugitive emissions from valves,prv's N/A N/A
IF-09 and flanges
IF-11 Fiber takeup N/A N/A
IF-12 Maintenance solvents N/A N/A
IF-15 Spray condenser recycle feed tank N/A N/A
IF-16 Polymer sump N/A N/A
IMPW Maintenance area parts washers N/A N/A
ITL Tire application lab N/A N/A

Page 36 of 41
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Emission Source Control Device Control/Recovery
ID No. Emission Source Description tr No. Device Description
ALAN III ESTERIFICATION
Three esterification reactors in series(APT 101A, Recovery Device
APT104A,and APT107A) Cl 10A/ Surface
ESO 1 C H I A condenser/spare
PSD Recovered condensate goes to ethylene glycol recycle venting to
NSPS DDD* at CL2
MACT JJJ C112A/ Control Device
Wastewater goes to prefinish Alan III seal pot(VT- C113A Direct contact
532A then to hotwells 1-1720513/1-1720613) barometric
condenser/spare
ALAN IV ESTERIFICATION
Three esterification reactors in series(APT 101B, Recovery Device
APT10413,and APT10713) C 1 1 OB/ Surface
C 1 1 1 B condenser/spare
ES02 Recovered condensate goes to ethylene glycol recycle venting to
PSD at CL2
MACT JJJ C 112B/ Control Device
Wastewater goes to prefmish Alan IV seal pot(VT- C 113B Direct contact
532B then to hotwells HT205B/HT206B) barometric
condenser/spare
ALAN III PREPOLYCONDENSATION
ES12 First stage reactor APT 114A vents through Recovery Device
PSD * barometric condenser and liquid ring vacuum C 124A/ Direct contact
NSPS DDD pump(s) C 125A barometric spray
MACT JJJ condenser/spare
ES13 Second stage reactor APT117A vents through Recovery Device
PSD * barometric condenser and liquid ring vacuum C 122A/ Direct contact
NSPS DDD C 123A barometric spray
MACT JJJ pp(s) condenser/spare
ES21 Direct contact barometric condenser receiver
PSD HT126A
NSPS DDD* NA N/A
NSPSMAC JJJ Ethylene glycol/water goes to storage tank HT-10
then to ethylene glycol recycle CL2
ALAN IV PREPOLYCONDENSATION
ES 14 First stage reactor APT 114B vents through Recovery Device
PSD barometric condenser and liquid ring vacuum C 124B/ Direct contact
MACT JJJ pump(s) C125B barometric spray
condenser/spare
ES 15 Second stage reactor APT117B vents through Recovery Device
PSD barometric condenser and liquid ring vacuum C12213/ Direct contact
C123B barometric spray
MACT JJJ pumps) condenser/spare

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%6 Emission Source Emission Source Descri ton Control Device Control/Recovery
SID No. p ID No. Device Description
t Direct contact barometric condenser receiver
ES22 HT 126B
PSD NA N'A
MACT JJJ Ethylene glycol/water goes to storage tank HT-10
then to ethylene glycol recycle CL2
ALAN III POLYMERIZATION
APT201A - Prefinish reactor(with process ejectors)feeding three
PSD final finish reactors with multiple stage process
NSPS,DDD* ejector assemblies and intercondensers venting to seal N/A N-`A
MACT JJJ pots HT205A/HT206A
APT301A Final finish reactor with multiple stage steam ejectors
PSD * and intercondensers venting to seal pots N/A N'A
NSPS DDD HT305A/HT306A
MACT JJJ
APT401 A Final finish reactor with multiple stage steam ejectors
PSD * and intercondensers venting to seal pots WA N'A
NSPS DDD HT405A/HT406A
MACT JJJ
SD P Final finish reactor with multiple stage steam ejectors
PSD and intercondensers ventingto seal pots N,'A N;'A
MACT JJJ
NSPS DDD* HT605A/I-IT606A
ALAN IV POLYMERIZATION
J Prefinish reactor(with process ejectors)feeding three
` APT20113 - final finish reactors with multiple stage process
PSD MALT JJJ ejector assemblies and intercondensers venting to seal N/A N/A
pots HT205B/HT206B
APT301B Final finish reactor with multiple stage steam ejectors
h PSD and intercondensers venting to seal pots N%A N/A
MACT JJJ HT305B/HT306B
g APT401 B Final finish reactor with multiple stage steatn ejectors
PSD and intercondensers venting to seal pots N%A N/A
MACT JJJ HT405B/HT406B
r APT501 Final finish reactor with multiple stage steam ejectors
PSD and intercondensers venting to seal pots N/A N/A
MACT JJJ HT505B/HT506B
ETHYLENE GLYCOL RECOVERY CLI
Distillation column CL1
ES26CL 1 Bottoms ethylene glycol goes to spent glycol storage Control Device
PSD Overheads surface
NSPS DDD* tank IVT-20. C 127 condenser venting to
MACT JJJ seal pot VT-41
Overheads wastewater is used in direct contact
condensers at Alan III esterification.

Current Student Schedule nnps:iiseiiservice.uncacuu/piziintu-4rn%-,,Liuwa =ate•__
2014 Ellucian Company L.P. and its affiliates.
2 of 2 8/14/2014 10:48 PM

Emission Source Emission Source Description Control Device ControVRecovery
ID No. ID No. Device Description
M
ETHYLENE GLYCOL RECYCLE CL2
O ES24 Spent ethylene glycol feed tank HT-10 N/A N/A
PSD
Recovery Device
C 143 Surface condensers
ES26CL2 Distillation column CI-2 and overheads seal pot
PSD NSPS DDD* Bottoms ethylene glycol is returned to the process. VT-87
Control Device
MACT JJJ Overheads wastewater is sent to the cooling tower. C 128 Side stream overheads
direct contact
nl condenser
n ES23 Ethylene glycol bottoms tank HT- I N/A N/A
PSD
WASTEWATER
HT205A/
HT206A Alan III prefinish reactor seal pots(hotwell for N/A N/A
MACT JJJ intercondensers and water seal for final vacuum vent)
T305A/ Alan III final finish reactor seal pots(hotwell for
HT306A intercondensers and water seal for final vacuum vent) N/A N/A
MACT JJJ
HT405A/ Alan III final finish reactor seal pots(hotwell for
HT406A intercondensers and water seal for final vacuum vent) N/A N/A
MACT JJJ
HT605A/ Alan III final finish reactor seal pots(hotwell for
HT606A intercondensers and water seal for final vacuum vent) N/A N/A
MACT JJJ
° HT205B/ Alan IV prefinish reactor seal pots(hotwell for
HT206B intercondensers and water seal for final vacuum vent) N/A N/A
MACT JJJ
HT305B/ Alan IV final finish reactor seal pots(hotwell for
M HT306B intercondensers and water seal for final vacuum vent) N/A N/A
MACT JJJ
HT405B/
� HT406B Alan IV final finish reactor seal pots(hotwell for N/A N/A
MACT JJJ intercondensers and water seal for final vacuum vent)
HT505B/ Alan IV final finish reactor seal pots(hotwell for
HT506B intercondensers and water seal for final vacuum vent) N/A N/A
MACT JJJ
VP135A Alan III prepolycondensation vacuum pump cooling N/A N/A
MACT JJJ water
VP136A Alan III prepolycondensation vacuum pump cooling N/A N/A
MACT JJJ water
VP137A Alan III prepolycondensation vacuum pump cooling N/A N/A
MACT JJJ water

ra�G � u� �

Emission SourceI F Emission Source Description Control Device Control/Recovery
ID No. ID No. Device Description
VP138A Alan III prepolycondensation vacuum pump cooling N/A N/A
MACT JJJ water
VP135B Alan IV prepolycondensation vacuum pump cooling N/A N/A
MACT JJJ water
VP136B Alan IV prepolycondensation vacuum pump cooling N/A N/A
MACT JJJ water
VP13713 Alan IV prepolycondensation vacuum pump cooling N/A N/A
MACT JJJ water
VP13813 Alan IV prepolycondensation vacuum pump cooling N/A N/A
MACT JJJ water
C112A/
C 113A Direct contact condensate from Alan III esterification N/A N/A
MACT JJJ
C11213/
Cl 13B Direct contact condensate from Alan IV esterification N/A N/A
MACT JJJ
C127 CLI overheads surface condenser seal pot IVT-41 N/A N/A
MACT JJJ used in direct contact condensers for esterification
C 128 Side stream CL2 overheads direct contact condenser N/A N/A
MACT JJJ sent to cooling tower
COOLING TOWERS
TW2
,may PSD Marley process cooling tower units 11, 12,and 13 N/A N/A
MACT JJJ
NSPS DDD*
TW3
PSD Marley process cooling tower units 14, 15,and 16 N/A N/A
MACT JJJ
NSPS DDD*
SPINDRAW OPERATIONS
ES I OA Six spin draw operations for Alan III polymer Control Device
PSD production MISTEI Condenser/mist
eliminator
ES 10B Six spin draw operations for Alan IV polymer Control Device
PSD production MISTE2 Condenser/mist
eliminator
UTILITIES
SG 1 Natural gas/No.6 fuel oil-fired boiler(64.2 million
D.1109 case by Btu per hour maximum heat input rate) N/A N/A
case MACT
SG2 Natural gas/No.6 fuel oil-fired boiler(64.2 million
213.1109 case by Btu per hour maximum heat input rate) N/A N/A
case MACT
t
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f
00 Emission Source Emission Source Description Control Device Control/Recovery
ID No. ID No. Device Description
SG3
NSPS Dc Natural gas-fired boiler(37.8 million Btu per hour N/A N/A
2D.1109 case by maximum heat input rate)
case MACT
HE553
NSPS Dc Natural gas/propane-fired steam superheater(10
2D A 109 case by million Btu per hour maximum heat input rate) N/A N/A
case MACT
HE554
NSPS Dc Natural gas/propane-fired steam superheater(10 N/A N/A
2D.1109 case by million Btu per hour maximum heat input rate)
case MACT
HE3 Natural gas/No.6 fuel oil-fired Dowtherm heater
2D.1109 case by (16.8 million Btu per hour maximum heat input rate) N/A N/A
case MACT
HE4 Natural gas/No.6 fuel oil-fired Dowtherm heater
� 2D.1109 case by (16.8 million Btu per hour maximum heat input rate) N/A N/A
case MACT
HE5 Natural gas/No. 6 fuel oil-fired Dowtherm heater
213.1109 case by (16.8 million Btu per hour maximum heat input rate) N/A N/A
case MACT
F07 Dowtherm Transfer and Storage N/A N/A

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Billing Summary
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Transaction ID 1104348658
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p-DrA
�goovdz
Performance
June 25, 2014
NC DENR Raleigh Regional Office
Air Emission Inventory
Raleigh Regional Office
NC Department of Environment and Natural Resources
3800 Barrett Drive
Raleigh, North Carolina 27609
RE: 2013 Point Source Air Pollutant Emissions Inventory
Performance Fibers, Inc.
New Hill, North Carolina
Air Quality Permit No. 02657T28
Enclosed is one (1) copy of the Point Source Air Pollutant Emissions Inventory
for the Performance Fibers, Inc. facility located in New Hill, Chatham County,
North Carolina. The inventory represents the best estimate of actual stack and
fugitive emissions for the 2013 calendar year and includes a Certification Form,
signed by the legally responsible official at the facility, along with supporting
emission calculations.
All the required information was submitted electronically on June 18, 2014,
utilizing the DAQ internet-based reporting tool, Air Emissions Reporting Online
(AERO).
If you should have any questions regarding this submission, please contact me.
Sincerely,
T 1-
Marty R. Stewart
Regional Environmental Leader
Office: [phone]
Fax: [phone]
Email: [e-mail]
Enclosure: 1 Binder
3 3 8 PEA RIDGE ROAD I NEW HILL , NC 2 7 5 6 2 T E L 9 1 9 5 4 2 2 2 0 0
www.performancefibers.com

COPY of RECORD Date Submitted: 6/18/2014 10:03:56
Inventory Certification Form(Title V)
Facility Name: Performance Fibers,Inc. Facility ID : 1900002
338 Pea Ridge Road Permit : 02657
New Hill,NC 27562 County : Chatham
DAQ Region : RRO
North Carolina Department of Environment and Natural Resources
Division of Air Quality
Air Pollutant Point Source Emissions Inventory—Calendar Year 2013
These forms must be completed and returned even if the facility did not operate or emissions were zero
The legally defined "Responsible Official" of record for your facility is Don Peterson
This person or one that meets the definition below must sign this certification form.
The official submitting the information must certify that he/she complies with the requirements as specified in Title 15A
NCAC 2Q.0520(b)which references and follows the federal definition.40 CFR Part 70.2 defines a responsible as meaning one
of the following:
1. For a corporation: a president, secretary,treasurer, or vice—president of the corporation in charge of a principal
business function, or any other person who performs similar policy or decision making functions for the overall
operation of one or more manufacturing,production, or operating facilities applying for a or subject to a permit and
either
i. the facilities employ more than 250 persons or have gross annual sales or expenditures exceeding$25
million(in second quarter 1980 dollars); or
ii. the delegation of authority to such representatives is approved in advance by the permitting authority;
2. For partnership or sole propietorship; a general partner or the proprietor,respectively;
3. for a muncipality, state,federal,or other public agency includes the chief executive officer having responsibility for the
overall operations of a principal geographic unit of the agency(e.g.,a Regional Administrator of EPA).
CLRTIFICATIONT•
(Important: Legally Resgon5ible Official,read and sign gfter allrfinaLl
certify that I am the responsible official for this facility,as described above,and hereby certify that the information contained
in this air emissions report,including attached calculations and documentation, is true, accurate and complete. (Subject to legal
enalities of up to$25,000 per occurrence and possible imprisonment as outlined in G.S.§143-215.3(a)(2))
Responsible Official's Signature Below use blue ink): Date Signed:
Printed Name: Do rson
Si ature: � -ZK-t�
This form applies to Title V facilities. If this facility is not classified as Title V,please telephone your regional office Emission
Inventory contact at once for proper forms.
Email address of Responsible Official: C�o�41d, p e}u;o P.�- ,, N a.tca b cv.v► l
Information on this Form cannot be held confidential
1p
IV-
COPY of RECORD Date Submitted: 6/18/2014 10:03:56 1

2013 FACILITY WIDE EMISSION SUMMARY
��Citeria Pita �3 a � WIR� D
iy 4 y §'y t C+�"a.:.,w... `a.:�d.. .> \ 1 it r �� x .��' .. .�," •�.•, x I �.N+.
Carbon Monoxide(CO) 23.33 19.97 -14.4 ES03-05;ES06-08;ES11;ES20;ES27-28;ES32-33;IEG-2;IEG-3
Nitrogen Oxides(NOx) 28.05 24.11 -14.0 ES03-05;ES06-08;ES11;ES20;ES27-28;ES32-33;IEG-2;IEG-3
Total Particulate Matter(PM) 11.35 10.75 -5.3 ES03-05;ES06-11;ES20;ES27-28;ES32-33:F10;IEG-2;IEG-3
PM-10 11.35 10.75 -5.3 ES03-05;ES06-11;ES20;ES27-28;ES32-33:F10;IEG-2;IEG-3
PM-2.5 11.35 10.75 -5.3 ES03-05;ES06-11;ES20;ES27-28;ES32-33:F10;IEG-2;IEG-3
Sulfur Dioxide(S02) 0.27 0.27 1.5 ES03-05;ES06-08;ES11;ES20;ES27-28;ES32-33;IEG-2;IEG-3
Total VOUTOC incl.HAP 130.79 141.38 8.1 All Except ES10 F05&F10
:v 3,�•t-��� �"s � � � � ads
tirission Suummary Oatttyr�
xr��•s>..r,N,..:.�� ..8'`.* '�,€��..��. :a s.� ...��, �� xn.�.... �Ditlerert�,,..- ��€,:;���...... -. �*" a..,•,._ �.r .>a.���.,�� v.r.,•.
Carbon Dioxide(CO2) 33,238 28,414 -14.5 ES03-05;ES06-08;ES11;ES20;ES27-28;ES32-33;IEG-2;IEG-3
Methane(CH4) 0.64 0.54 -14.5 ES03-05;ES06-08;ES27-28;ES32-33;IEG-2;IEG-3
Nitrous Oxide N20 0.61 0.52 -14.5 ES03-05•ES06-08•ES27-28•ES32-33•IEG-2;IEG-3
> �
... ........'� �.S€...�. +,a a, „•.. �• �`�.�,n� °.' .:F.\.. �3ff�C9riiC� ..... .i.� �. wx'� . %a.
Acetaldehyde 2,826.97 1,288.07 -54.4 ES01-02;ES11;ES20-22;ES26;ES29;F11;F15-16 ,
Acetic Acid 22.70 28.77 26.7 F11
Acrolein 0.01. 0.02 22.3 ES11;ES20
Acrylic Acid 0.00 0.00 NA F12
Antimony Compounds 405.45 399.90 -1.4 ES03-09
Arsenic Compounds 0.11 0.10 -14.3 ES03-08; ES27-28;ES32-33
Benzene 9.04 8.91 -1.5 ES03-08;ES11;ES20;ES27-28;ES32-33;IHT-15;IHT-21
Beryllium Compounds 0.01 0.01 -14.4 ES03-06;ES27-28;ES32-33
Biphenyl 596.38 4,583.30 668.5 F06
Butadiene,1,3- 0.01 0.01 22.3 ES11;ES20
Butylene Oxide,1,2- 2.64 2.05 -22.4 F12
Cadmium Compounds 0.61 0.52 -14.5 ES03.08;ES27-28;ES32-33
Chromium Compounds 0.78 0.66 -14.5 ES03-08;ES27-28;ES32-33
Chromium VI 0.00 0.00 28.7 ES03-04;ES06-08
Cobalt Compounds 0.05 0.04 -12.0 ES03-08;ES27-28;ES32-33
Cumene 0.58 0.58 0.0 IHT-15;IHT-21
Dichlorobenzene,1,4- 0.66 0.57 -14.5 ES03-08;ES27-28;ES32-33
Dioxane,1,4- 80.91 80.84 -0.1 ES09;F07;FO6;F11;F15;F16
Ethylbenzene 0.58 0.58 0.0 ES03-08;IHT-15;IHT-21
Ethylene Glycol 234,461.18 245,724.86 4.8 ES01-02;ES09;ES16-ES18;ES21-22;ES26;ES29-30;FO1-FO4;
F07-FO9;F11-12;F15:IVT-1
Fluorides 0.02 0.02 28.7 ES03-08
Formaldehyde 52.13 46.14 -11.5 ES03-08;ES11;ES20;ES27-28;ES32-33;ITL
Hexane 1,064.00 914.40 -14.1 ES03-08;ES27-28;ES32-33;F12;IHT-15;IHT-21
Lead Compounds 0.28 0.24 -14.4 ES03-08;ES27-28;ES32-33
Manganese Compounds 0.21 0.18 -14.2 ES03-08;ES27-28;ES32-33
Mercury Compounds 0.14 0.12 -14.5 ES03-08;ES27-28;ES32-33
Methanol 9.69 4.46 -53.9 F11
Naphthalene 0.36 0.32 -12.7 ES03-08;ES11;ES20;ES27-28;ES32-33;IHT-15;IHT-21
Nickel Compounds 1.20 1.05 -13.1 ES03-08;ES27-28;ES32-33
Polycyclic Organic Matter(POM) 0.06 0.06 -6.3 ES03-08;ES11;ES20;ES27-28:ES32-33
Selenium Compounds 0.01 0.01 -13.5 ES03-08;ES27-28;ES32-33
Styrene 0.10 0.10 0.0 IHT-15;IHT-21
2,2,4-Trimethylbenzene 3.95 3.95 0.0 IHT-15;IHT-21
Toluene 12.99 12.74 -2.0 ES03-09;ES11;ES20;ES27-28;ES32-33;IHT-15;IHT-21
Trichloroethylene 498.02 386.55 -22.4 F12
Vinyl Acetate 2.06 2.62 26.7 F11
X lenes 2.22 2.23 0.5 ESO3-08•ES11:ES20:IHT-15;IHT-21
\., s
dNnn4v one >� \�
�2013 a \z \\
.
�s Differ anc.,, .• .,z
Chlorodifluoromethane 1.02 3.58 250.0 F12
Dichlorodifluoromethane 0.00 0.00 NA F05
1,1-Dichloro-1-fluoroethane 0.00 0.00 NA F12
Methyl chloroform 0.00 0.00 28.7 ES03-08;F12
1.1,1,2-Tetrafluoroethane 96.60 92.40 -4.3 F05;F12
Trichlorofluoromethane 350,00 600.00 71.4 F05
Trichlorotrifluoroethane 3.07 10.74 250.0 F12
6/24/2014 AEI Calculations 2013

ES01 - Alan III Esterification Vessels
*Test 2013 Actual Emissions
Pollutants CAS No. Emission Data Entry for GR-7 /zJ o/- 4 fT i c 14
Ib/hr Ib/ r ton/ r 65c t - APT/0 4,4
Acetaldehyde 75-07-0 0.0336 285.47 1.43E-01 ' f� C 3o / _ 4P'r I v 7 /d
15iethyfenv Glycol 111-46-6 5.79E-05 0.49 2.46E-04
Ditseprorpylamine 108-18-9 0.150 1,274.40 6.37E-01
Ethylene Glycol 107-21-1 1.08E-03 9.18 4.59E-03
2-Methyl-1,3-Dioxolane 497-26-7 0.0616 523.35 2.62E-01
P opene 115-07-1 0.175 1,486.80 7.43E-01
VOC 0.4213 3,579.69 1.79
Year: 2013
Total Production Hours: 8,496 hr/yr
Average C 112A Exit Gas Temperature: <120 F
Determined by condenser vent testing on Alan III (see ENTROPY, INC. Stationary source sampling report Reference No. 16350 July 1997) i
6/24/2014 AEI Calculations 2013

ES02 - Alan IV Esterification Vessels
*Test 2013 Actual Emissions
Pollutants CAS No. Emission
Ib/hr IbJ r ton/ r © S 576
Acetaldehyde 75-07-0 0.0336 0.00 0.00E+00
Diethylene Glycol 111-46-6 5.79E-05 0.00 0.00E+00 5 0 —4geT /0/!3
Diisopropylamine 108-18-9 0.150 0.00 0.00E+00 _ r SO f�'? 10 y ,S
Ethylene Glycol 107-21-1 1.08E-03 0.00 0.00E+00
2-M ethyl-1,3-Dioxolane 497-26-7 0.0616 0.00 0.00E+00 _ lr S p -/}FT d -;0'- i3
Propene 115-07-1 0.175 0.00 0.00E+00
VOC 0.4213 1 0.00 1 0.00
Year: 2013
Alan IV Production Hours: 0 hr/yr
Average C 113B Exit Gas Temperature: 108 F
Determined by condenser vent testing on Alan III (see ENTROPY, INC. Stationary source sampling report Reference No. 16350 July 1997)
6/24/2014 AEI Calculations 2013

ES03,ESO4,ES05-Steam Generatina Boilers(SG-1,SG-2,SG-3)
SG-1
C� 5
Emission Factor Emission Factor for Emissions From No.Emissions From No. Emissions From Emissions From O
Pollutant for No.6 Fuel Oil Natural Gas Total Emissions Total Emissions 6 Fuel Oil ONLY 6 Fuel Oil ONLY Natural Gas ONLY Natural Gas ONLY
From SG-1(lb/yr) From SGA(ton/yr)
(Ibl gal) (Ib/mmc f) (Iblyr) (ton/yr) (Iblyr) (tonlyr) O CJ f
�^9.5- �+,,ar: -a? ,,;a., ".- �ix�s1,*,x_.. (�
Total PM 2.27E-02 7.6 994.78 0.50 - 13.93 0.01 980.85 0.49
Filterable PM-10 1.95E-02 7.6 992.83 0.50 11.98 0.01 980.85 0.49 5 G 1
Filterable PM-2.5 1.27E-02 7.6 988.65 1 0.49 7.81 0.00 980.85 0.49
NOx 5.50E-02 100 12 939.67 6.47 33.77 0.02 12 905.90 6.45
CO 5.00E-03 84 10 844.03 5.42 3.07 0.00 10 840.96 5.42 .` C Z
S02 3.30E-01 0.6 279.87 0.14 202.44 0.10 77A4 0.04 �I
VOC 2.80E-04 5.5 710.00 0.35 0.17 0.00 709.82 0.35 C
Total HAP 1.83E-04 1.89 243.84 0.12 0.11 0.00 243.72 0.12 J
Largest HAP 8.45E-05 1.80 232.36 0.12 0.05 0.00 232.31 0.12
CO2 2.50E+01 120,000 15,502 430 7,751 15,350 1 1 15 487,080 17 744
CH4 1.00E-03 2.30 297.45 0.15 0.61 1 0.00 1 296.84 0.15
N20 1.10E-04 2.20 284.00 0.14 0,07 1 0,00 1 283,93 0.14
Antimon 5.25E-06 0 3.22E-03 1.61E-06 3.22E-03 1.61E-06 0.00E+00 0.00E+00
Arsenic 1,32E-06 2.00E-04 2.66E-02 1.33E-05 8.10E-04 4.05E-07 2.58E-02 1.29E-05
Benzene 2.14E-07 2.10E-03 2.71E-01 1.36E-04 1.31E-04 6.57E-08 2.71E-01 1.36E-04
Beryllium 2.78E-08 1.20E-05 1.57E-03 7.83E-07 1.71E-05 8.53E-09 1.55E-03 7.74E-07
Cadmium 3.98E-07 1.10E-03 1.42E-01 7.11E-05 2.44E-04 1.22E-07 1.42E-01 7.10E-05
Chromium 8.45E-07 1.40E-03 1.81E-01 9.06E-05 5.19E-04 2.59E-07 1.81E-01 9.03E-05
Chromium VI 2.48E-07 0 1.52E-04 7.61E-08 1.52E-04 7.61E-08 0.00E+00 0.00E+00
Cobalt 6.02E-06 8.40E-05 1.45E-02 7.27E-06 3.70E-03 1.85E-06 1.08E-02 5.42E-06
Dichlorobenzene-1,4 0 1.20E-03 1.55E-01 7.74E-05 O.00E+00 0.00E+00 1.55E-01 7.74E-05
Eth(benzene 6.36E-08 0 3.91E-05 1.95E-08 3.91E-05 1.95E-08 O.00E+00 0.00E+00
Fluoride 3.73E-05 0 2.29E-02 1.15E-05 2.29E-02 1.15E-05 0.00E+00 O.00E+00
Formaldehyde 3.30E-05 7.50E-02 9.70E+00 4.85E-03 2.03E-02 1.01E-05 9.68E+00 4.84E-03
Hexane 0 1.8 2.32E+02 1.16E-01 O.00E+00 0.00E+00 2.32E+02 1.16E-01
Lead 1.51E-06 5.00E-04 6.55E-02 3.27E-05 9.27E-04 4.64E-07 6.45E-02 3.23E-05
Manganese 3.00E-06 3.80E-04 5.09E-02 2.54E-05 1.84E-03 9.21E-07 4.90E-02 2.45E-05
Mercury 1.13E-07 2.60E-04 3.36E-02 1.68E-05 6.94E-05 3.47E-08 3.36E-02 1.68E-05
Methyl chloroform 1 1 1-Trichloroethane 2.36E-07 0 1.45E-04 7.25E-08 1.45E-04 7.25E-08 O.00E+00 0.00E+00
Naphthalene 1,13E-06 6.10E-04 7.94E-02 3.97E-05 6.94E-04 3.47E-07 7.87E-02 3.94E-05
Nickel 8.45E-05 2.10E-03 3.23E-01 1.61E-04 5.19E-02 2.59E-05 2.71E-01 1.36E-04
POM 1.20E-06 8.82E-05 1.21E-02 6.06E-06 7.37E-04 3.68E-07 1.14E-02 5.69E-06
Selenium 6.83E-07 2.40E-05 3.52E-03 1.76E-06 4.19E-04 2.10E-07 3.10E-03 1.55E-06
Toluene 6.2E-0 06 3.40E-03 4.43E-01 2.21E-04 3.81E-03 1.90E-06 4.39E-01 2.19E-04
0-X lane 1.09E-07 0 6.69E-05 3.35E-08 6.69E-05 3.35E-08 0.00E+00 0.00E+00
2011
No.6 Fuel Usage From SGA(gal/yr) 614 Natural Gas POM Emission Factor
No.6 Fuel Usage From SG-2(gaVyr) 5 Calculation(from AP-42)
Total No.6 FO(SG-1+SG-2) 619 2-Methylnaphthalene 2.40E-05
3-Methylchloranthrene 1.80E-06
Natural Gas Usage From SG-1(mmcf/yr) 129.06 7,12-Dimethylbenz(a)anthracene 1.60E-05
Natural Gas Usage From SG-2(mmcf/yr) 112.64 Acenaphthene 1.80E-06
Natural Gas Usage From SG-3(mmcf/yr) 59.30 Acenaphthylene 1.80E-06
Total NG(SG-1+SG-2+SG-3) 301.00 Anthracene 2.40E-06
Benz(a)anthracene 1.80E-06
SG-1 Nat Gas Emissions ONLY(lb/yr) 28196.41 Benzo(a)pyrene 1.20E-06
SG-1 No.6 Fuel Oil Emissions ONLY(lb/yr) 273.45 Benzo(b)Buoranthene 1.80E-06
Benzo(g,h,i)peryiene 1.20E-05
SG-1 Total Emissions in(Ib/yr) 28469.86 Benzo(k)8uoranthene 1.80E-06
Chrysene 1.80E-06
SG-2 Nat Gas Emissions ONLY(lb/yr) 24609.90 Dibenzo(a,h)anthracens 1.20E-06
SG-2 No.6 Fuel Oil Emissions ONLY(Ib/yr) 2.23 Fluoranthene 3.00E-06
Fluorene 2.80E-06
SG-2 Total Emissions(Ib/yr) 24612.12 Indeno(1,2,3-cd)pyrene 1.80E-06 V
Phenanathrene 1.70E-05
SG-3 Nat Gas Emissions ONLY(Ib/yr) 12954.59 Pyrene 5.00E-06
SG-3 No.6 Fuel Oil Emissions ONLY(lb/yr) NA
TOTAL POM 8.82E-05
SG-3 Total Emissions(Ib/yr) 12954.59
2013%S in No.6 Fuel Oil(average) 2.10
6/24/2014 AEI Calculations 2013

ES03,ESO4,ES05-Steam Generatina Boilers(SG-1,SG-2,SG-3)
SG-2
Emission Factor Emission Factor for Total Emissions Total Emissions Emissions From No.Emissions From No. Emissions From Emissions From
Pollutant for No.6 Fuel Oil Natural Gas From SG-2 Emiss(Iblyrions
From l Emissions
sions 6 Fuel Oil ONLY 6 Fuel Oil ONLY Natural Gas ONLY Natural Gas ONLY
(Ib/gal) (lb/mmcf) (lb/yr) (ton/yr) (lb/yr) (ton/yr)
Criteria Air Pollutants
Total PM 2.27E-02 Z6 856.20 0.43 0.11 0.00 856,09 0.43
Filterable PM-10 1.95E-02 7.6 856,18 0.43 0.10 0.00 856.09 0.43
Filterable PM-2.5 1.27E-02 7.6 856,15 0,43 0.06 0.00 855.09 0.43
NOx 5.50E-02 100 11,264,58 5.63 0.28 0.00 11264.30 5.63
CO 5.00E-03 84 9.462.04 4.73 0.03 0.00 9,462.01 4.73
802 3.30E-01 0.6 69.23 0.03 1.65 0.00 67.59 0.03
VOC 2.80E-04 5.5 619,54 0.31 0.00 0.00 619.54 0,31
Total HAP 1.83E-04 1.89 212,72 0.11 0.00 0.00 212.72 0.11
Largest HAP 8.45E-05 1.80 202.76 0.10 0.00 0 00 202.76 0.10
Greenhouse Gas GHG Emissions
CO2 2.50E+01 120,000 13.517285 6,759 125 0 13,517,160 6,759
CH4 1.00E-03 2,30 259 OS 0.13 0.01 000 259.08 0.13
N20 1.10E-04 2.20 247.82 0.12 0.00 0.00 247.81 0.12
Toxic/Hazardous Air Pollutants
Antimony 5.25E-06 0 2.63E-05 1.31E-08 0,00 1.31E-08 0.00E+00 0.00E+00
Arsenic 1.32E-06 2.00E-04 2.25E-02 1.13E-05 0,00 3.30E-09 2.25E-02 1.13E-05
Benzene 2.14E-07 2.10E-03 2.37E-01 1.18E-04 0.00 5.35E-10 2.37E-01 1.18E-04
Beryllium 2.78E-08 1.20E-05 1.35E-03 6.76E-07 0.00 6.95E-11 1.35E-03 6.76E-07
Cadmium 3.98E-07 1.10E-03 1.24E-01 6.20E-05 0.00 9.95E-10 1.24E-01 6.20E-05
Chromium 8.45E-07 1.40E-03 1.58E-01 7.89E-05 0,00 2.11E-09 1.58E-01 7,89E-05
Chromium VI 2.48E-07 0 1.24E-06 6.20E-10 0.00 6.20E-10 0.00E+00 0.00E+00
Cobalt 6.02E-06 8.40E-05 9.49E-03 4.75E-06 0,00 1.51E-08 9.46E-03 4.73E-06
Dichlorobenzene-1,4 0 1.20E-03 1.35E-01 6.76E-05 0,00 0.00E+00 1.35E-01 6.76E-05
Eth(benzene 6.36E-08 0 3.18E-07 1.59E-10 0,00 1.59E-10 0.00E+00 O.00E+00
Fluoride 3.73E-05 0 1.87E-04 9.33E-08 0,00 9.33E-08 0.00E+00 0.00E+00
Formaldehyde 3.30E-05 7.50E-02 8.45E+00 4.22E-03 0,00 8.25E-08 8.45E+00 4.22E-03
Hexane 0 1.8 2.03E+02 1.01E-01 0,00 O.00E+00 2.03E+02 1.01E-01
Lead 1.51E-06 5.00E-04 5.63E-02 2.82E-05 0.00 378E-09 5.63E-02 2.82E-05
Manganese 3.00E-06 3.80E-04 4.28E-02 2.14E-05 0.00 7.50E-09 4.28E-02 2.14E-05
Mercury 1.13E-07 2.60E-04 2.93E-02 1.46E-05 0.00 2.83E-10 2.93E-02 146E-05
Methyl chloroform 1 1 1-Trichloroelhane 2.36E-07 0 1.18E-06 5.90E-10 0.00 5.90E-10 0.00E+00 0.00E+00
Naphthalene 1.13E-06 6.10E-04 6.87E-02 3.44E-05 0.00 2.83E-09 6.87E-02 3.44E-05
Nickel 8.45E-05 2.10E-03 2.37E-01 1.18E-04 0.00 2.11E-07 2.37E-01 1.18E-04
POM 1.20E-06 8.82E-05 9.94E-03 4.97E-06 0.00 3.00E-09 9.94E-03 4.97E-06
Selenium 6.83E-07 2.40E-05 2.71E-03 1.35E-06 0,00 1.71E-09 2.70E-03 1.35E-06
Toluene 6.20E-06 3.40E-03 3.83E-01 1.92E-04 0.00 1.55E-08 3.83E-01 1.91E•04
o-X lane 1.09E-07 0 5.45E-07 2.73E-10 0.00 2.73E-10 0.00E+00 0.00E+00
2011
No.6 Fuel Usage From SG-1(gal/yr) 614
No.6 Fuel Usage From SG-2(gal/yr) 5
Total No.6 FO(SG-1+SG-2) 619
Natural Gas Usage From SG-1(mmcf/yr) 129.06
Natural Gas Usage From SG-2(mmcf/yr) 112.64
Natural Gas Usage From SG-3(mmcf/yr) 59.30
Total NG(SG-1+SG-2+SG-3) 301.00
SG-1 Nat Gas Emissions ONLY(lb/yr) 28196.41
SG-1 No.6 Fuel Oil Emissions ONLY(lb/yr) 273.45
SG-1 Total Emissions in(Iblyr) 28469.86
SG-2 Nat Gas Emissions ONLY(lb/yr) 24609.90
SG-2 No.6 Fuel Oil Emissions ONLY(lb/yr) 2.23
SG-2 Total Emissions(Iblyr) 24612A2
SG-3 Nat Gas Emissions ONLY(Iblyr) 12954.59
SG-3 No.6 Fuel Oil Emissions ONLY(lb/yr) NA
SG-3 Total Emissions(lb/yr) 12954.59
2013%S in No.6 Fuel Oil(average) 2.10
6/24/2014 AS Calculations 2013

ES03,ES04,ES05-Steam Generatina Boilers(SG-1,SG-2,SG-3)
SG-3
Emission Factor Emission Factor for Total 2012
Ponutant for No.6 Fuel Oil Natural Gas Total Emissions Total Emissions Total 2012 Actual Actual
(I.6 Fual) (Iblmmca From SG-3(Iblyr) From SG-3(ton/yr) Emissions(lb/yr) Emissions
(ton/yr)
Criteria Air Pollutants
Total PM 2.27E-02 7.6 450.64 0.23 2,301,62 1.15
Filterable PM-10 1.95E-02 7.6 450.64 0,23 2299.66 1.15
Filterable PM-2.5 1.27E-02 7.6 450.64 0.23 2 295.45 1.15
NOx 5.50E-02 100 5,929.50 2,96 30133.75 15.07
CO 5.00E-03 84 4,980.78 2,49 25,286.84 12.64
SO2 3.30E-01 0.6 35,58 0,02 384.68 0.19
VOC 2.80E-04 5.5 326.12 0.16 1,655.66 0.83
Total HAP 1.83E-04 1.89 111.98 0.06 568.53 0,28
West HAP 8.45E-05 1.80 106.73 0.05 541.85 0,27
CO2250E+01/ 120�00 7.115.400 3,558 36135.1 t5 18,068
CH4 1.00E-03 2.30 136 38 6.82E-32 692.91 3.46E-01
N2O 1.10E-04 2.20 130.45 6.52E-02 662.26 3 31 E-01
Antimony 5.25E-06 0 0.00 0.00E+00 3.25E-03 1.62E-06
Arsenic 1.32E-06 2.00E-04 0.01 5.93E-06 6.10E-02 3.05E-05
Benzene 2.14E-07 2.10E-03 0.12 6.23E-05 6.32E-01 3.16E-04
Beryllium 2.78E-08 1.20E-05 0,00 3.56E.07 3.63E-03 1.81E-06
Cadmium 3.98E-07 1.10E-03 0.07 3.26E-05 3.31E-01 1.66E-04
Chromium 8.45E-07 1.40E-03 0,08 4.15E.05 4.22E-01 2.11E-04
Chromium VI 2.48E-07 0 0.00 0.00E+00 1.54E-04 7.68E-08
Cobalt 6.02E-06 8.40E-05 0.00 2.49E-06 2.90E-02 1.45E-05
Dichlorobenzene-14 0 1.20E-03 0.07 3.56E-05 3.61E-01 1.81E-04
Eth(benzene 6.36E-08 0 0.00 0.00E+00 3.94E-05 1.97E-08
Fluoride 3.73E-05 0 0.00 O.00E+00 2.31E-02 1.15E-05
Fonnaldeh de 3.30E-05 7.50E-02 4.45 2.22E-03 2.26E+01 1.13E-02
Hexane 0 1.8 106,73 5.34E-02 5.42E+02 2.71E-01
Lead 1.51E-06 5.00E-04 0.03 1.48E-05 1.51E-01 7.57E-05
Manganese 3.00E-06 3.80E-04 0.02 1.13E-05 1.16E-01 5.81E-05
Mercury 1.13E-07 2.60E-04 0,02 7.71E-06 7.83E-02 3.92E-05
Methyl chloroform 1 1 1-Trichloroethane 2.36E-07 0 0.00 0.00E+00 1.46E-04 7.30E-08
Naphthalene 1.13E-06 6.10E-04 0.04 1.81E-05 1.84E-01 9.22E-05
Nickel 8.45E-05 2.10E-03 0.12 6.23E-05 6.84E-01 3.42E-04
POM 1.20E-06 8.82E-05 0.01 2.61E-06 2.73E-02 1.36E-05
Selenium 6.83E-07 2.40E-05 0,00 7.12E-07 7.65E-03 3.82E-06
Toluene 6.20E-06 3.40E-03 0.20 1.01E-04 1.03E+00 5.14E-04
o-X lens 1.09E-07 1 0 0.00 0.00E+00 6.75E-05 3.37E-08
2011
No.6 Fuel Usage From SG-1(gal/yr) 614
No.6 Fuel Usage From SG-2(gal/yr) 5
Total No.6 FO(SG-1+SG-2) 619
Natural Gas Usage From SG-1(mmcf/yr) 129.06
Natural Gas Usage From SG-2(mmcf/yr) 112.64
Natural Gas Usage From SG-3(mmcf/yr) 59.30
Total NG(SG-1+SG-2+SG-3) 301.00
SG-1 Nat Gas Emissions ONLY(Ib/yr) 28196.41
SG-1 No.6 Fuel Oil Emissions ONLY(lb/yr) 273.45
SG-1 Total Emissions in(Ib/yr) 28469.86
SG-2 Nat Gas Emissions ONLY(Iblyr) 24609.90
SG-2 No.6 Fuel Oil Emissions ONLY(Iblyr) 2.23
SG-2 Total Emissions(lb/yr) 24612.12
SG-3 Nat Gas Emissions ONLY(Ib/yr) 12954.59
SG-3 No.6 Fuel Oil Emissions ONLY(Iblyr) NA
SG-3 Total Emissions(Iblyr) 12954.59
2013%S in No.6 Fuel Oil(average) 2.10
IJN 6/24/2014 AEI Calculations 2013

Natural Gas POM Emission Factor Calculation(from AP-42)
2-Melhylnaphthalene 2.40E-05
3-Methylchloranthrene 1.80E-06
7,12-Dimethylbenz(a)anthracene 1.60E-05
Acenaphthene 1.80E-06
Acenaphthylene 1.80E-06
Anthracene 2.40E-06
Benz(a)anthracene 1.80E-06
Benzo(a)pyrene 1.20E-06
Benzo(b)fluoranthene 1.80E-06
Benzo(g,h,i)perylene 1.20E-06
Benzo(k)fluoranthene 1.80E-06
Chrysene 1.80E-06
Dibenzo(a,h)anthracene 1.20E-06
Fluoranthene 3.00E-06
Fluorene 2.80E-06
Indeno(1,2,3-cd)pyrene 1.80E-06
Phenanathrene 1.70E-05
Pyrene 5.00E-06
TOTAL POM 8.82E-05
Propane Sulfur Content
Sulfur content in propane calculated according to the maximum ethyl mercaptan content(50 ppm)
as provided in suppliers MSDS.
S + C21-16 -> C21-16S
50 lb C21-16S x 1 mole CAS x 1 mole S x 32 lb S
10 lb Propane 62 lb CAS 1 mole CAS 1 mole S
25.8 lb S
106lb Propane
_- 26 ppm S
_- 0.0026 wt.%S in Propane
25.8 lb S x 7,000 grains S x 11.9 lb Propane
106 Propane lb S 100ft3 Propane
= 2.1497 grains S
100 ft3 Propane
O
6/24/2014 AEI Calculations 2013

ES06,ES07,ES08-Dowtherm Heaters(HE-3,HE-4,HE-51
HE-3 I
"~
Emission Factor Emission Factor Total Emissions Emissions From Emissions From
HE-3 Natural HE-3 Natural
Pollutant for No.6 Fuel for Natural Gas From HE-3 Gas ONLY Gas ONLY
Oil(lb/gal) (lb/mmci) (lb/yr) H
(Ibtyr) (ton/yr)
Marla Air Pollutants
Total PM __ 2 27E-02 7.6 3623 36 23 002 �� I
Filterable PM-10 1.95E-02 T6 36.23 36.23 0.02
Filterable PM-2.5 1.27E-02 7.6 36.23 36,23 0,02
NOx 5.50E-02 100 476.70 476-70 0,24
CO 5.00E-03 84 400.43 400A3 0.20
S02 3.30E-01 0.6 2.86 2.86 0.00
VOC 2.80E-04 5.5 26.22 26.22 0.01
Total HAP 1.83E-04 1.89 9.00 9.00 0.00
Largest HAP 8 45E-05 1 80 1"1 8.58 0 00
Greenhouse Gas GHG)Emissions
702 2 50E«01 1 120,000 572.0401 572,040 286
CH4 1 OOE-03 2.30 10.96 10.96 D.01
N20 1 l OE-04 2 20 10491 10.49 0 01
Toxic/Hazardous Air Pollutants
Antimony 5.25E-06 0 0.00E+00 0.00E+00 0.00E+00
Arsenic 1.32E-06 2.00E-04 9.53E-04 9,53E-04 4.77E-07
Benzene 2.14E-07 2.10E-03 1.00E-02 1.00E-02 5.01E-06
Beryllium 2.78E-08 1.20E-05 5.72E-05 5.72E-05 2.86E-08
Cadmium 3.98E-07 1.10E-03 5.24E-03 5.24E-03 2.62E-06
Chromium 8.45E-07 1.40E-03 6.67E-03 6,67E-03 3.34E-06
Chromium VI 2.48E-07 0 0.00E+00 0.00E+00 O.00E+00
Cobalt 6.02E-06 8.40E-05 4.00E-04 4.00E-04 2.00E-07
Dichlorobenzene-1,4 0 1.20E-03 5.72E-03 5.72E-03 2.86E-06
Eth(benzene 6.36E-08 0 0.00E+00 0.00E+00 0.00E+00
Fluoride 3.73E-05 0 0.00E+00 0.00E+00 O.00E+00
Formaldehyde 3.30E-05 7.50E-02 3.58E-01 3.58E-01 1.79E-04
Hexane 0 1.8 8.58E+00 8.58E+00 4.29E-03
Lead 1.51E-06 5.00E-04 2.38E-03 2.38E-03 1.19E-06
Manganese 3.00E-06 3.80E-04 1.81E-03 1.81E-03 9.06E-07
Mercury 1.13E-07 2.60E-04 1.24E-03 1.24E-03 6.20E-07
Methyl chloroform 1,1,1-Trichloroethane 2.36E-07 0 0.00E+00 0.00E+00 0.00E+00
Naphthalene 1.13E-06 6.10E-04 2.91E-03 2.91E-03 1.45E-06
Nickel 8.45E-05 2.10E-03 1.00E-02 1.00E-02 5.01E-06
POM 1.20E-06 8.82E-05 4.20E-04 4.20E-04 2.10E-07
Selenium 6.83E-07 2.40E-05 1.14E-04 1.14E-04 5.72E-08
Toluene 6.20E-06 3.40E-03 1.62E-02 1,62E-02 8.10E-06
o-X lane 1.09E-07 0 0.00E+00 0.ODE+00 0.00E+00
2012
No.6 Fuel Oil Usage for HE-3(gal/yr) 0
No.6 Fuel Oil Usage for HE-4(gaVyr) 0
No.6 Fuel Oil Usage for HE-5(gal/yr) 5
Used Oil Consumption for HE-5(gal/yr) 0
Natural Gas Usage for HE-3(mmd/yr) 4.767
Natural Gas Usage for HE-4(mmcftyr) 75.299
Natural Gas Usage for HE-5(mmcf/yr) 68,413 148.479
HE-3 Total Natural Gas Emissions(Ibtyr) 1041.48
HE-3 No.6 Total Fuel Oil Emissions(Ibtyr) 0.00
Total HE-3 Emissions(Ibtyr) 1041.48
HE4 Total Natural Gas Emissions (lb/) 16451.0
HE-4 No.6 Total Fuel Oil Emissionss(Ibtyr) 0.000
Total HE-4 Emissions(Ibtyr) 16451.09
0-
HE-5 Total Natural Gas Emissions(Ibtyr) 14946.66
HE-5 No.6 Total Fuel Oil Emissions(Ibtyr) 2.23
Total HE-5 Emissions(Ibtyr) 14948.89
2013%S in No.6 Fuel Oil(average) 2.10
`\ 6/24/2014 AEI Calculations 2013

ES06,ES07,ES08-Dowtherm Heaters(HE-3,HE-4,HE-5)
HE-4
Emission Factor Emission Factor Emissions From Emissions From
Pollutant for No.6 Fuel for Natural Gas HE-4 Natural HE-4 Natural
Oil(lb/gal) (lb/mmcf) Gas ONLY Gas ONLY
(ib/yr). (tonlyr)
Criteria Air Pollutants
7cial71 227E-02 7.6 57227 _ 0.29
Filterable PM-10 1.95E-02 7.6 57227 0.29
Filterable PM-2.5 1.27E-02 7.6 572,27 0,29
NOx 5.50E-02 100 7,529.90 3.76,
CO 5.00E-03 84 6,325,12 316
S02 3.30E-01 0.6 45.18 402
VOC _ 2.80E-04 5.5 414.14 0.21
Total HAP 1.83E-04 1.82 142.20 0.07
Largest HAP 8 45E-05 1.80 135."l 0 07
s GHGEmissions *.
CO2 2.50E+01 120.000 9,035,680 4,518
CH4 1.00E-03 2 30 173.19 0,09
N20 1.10E-04 2 20 165,66 0.08
Antimony 5.25E-06 0 O.00E+00 0.00E+00
Arsenic 1.32E-06 2.00E-04 1.51E-02 7.,53E-06
Benzene 2.14E-07 2.10E-03 1.SBE-01 7.91E-05
Beryllium 2.78E-08 1.20E-05 9.04E-04 �4.52E-07
Cadmium 3.98E-07 1.10E-03 8.28E-02 4.14E-05
Chromium 8.45E-07 1.40E-03 1.05E-01 5.27E-05
Chromium VI 2.48E-07 0 O,OOEE«00 0.00E+00
Cobalt 6.02E-06 8.40E-05 6.33E-03 316E-06
Dichlorobenzene-1,4 0 1.20E-03 904E-02 4.52E-05
Eth(benzene 6.36E-08 0 0.00E+00 0 00E+00
Fluoride 3.73E-05 0 0.00E+00 -0 OOE+00
Formaldehyde 3.30E-05 7.50E-02 5.65E+00 2 82E-03
Hexane 0 1.8 1.36E+02 6.78E-02
Lead 1.51E-06 5.00E-04 3.76E-02 1.88E-05
Manganese 3.00E-06 3.80E-04 2.86E-02 1.43E-05
Mercury 1.13E-07 2.60E-04 1.96E-07 9.79E-06
Methyl chloroform 1,1,1-Tdchloroethane 2.36E-07 0 _ 0.GOE+00 0.00E+00
Naphthalene 1.13E-06 6.10E-04 4.59E-02 2.30E-05
Nickel 8.45E-05 2.10E-03 1.58E-01 j 7.91E-05
POM 1.20E-06 8.82E-OS 6.64E-03 3.32E-06
Selenium 6.83E-07 2.40E-OS 1.81E-03 9.04E-07
Toluene 6.20E-06 3.40E-03 I 2.56E-01 1.26E-04
o-X lane 1.09E-07 0 O,OOE+001 0 OGE+00
2012
No.6 Fuel Oil Usage for HE-3(gal/yr) 0
No.6 Fuel Oil Usage for HE-4(gaVyr) 0
No.6 Fuel Oil Usage for HE-5(gal/yr) 5
Used Oil Consumption for HE-5(gal/yr) 0
Natural Gas Usage for HE-3(mmcf/yr) 4.767
Natural Gas Usage for HE-4(mmcftyr) 75.299
Natural Gas Usage for HE-5(mmcftyr) 68.413 148.479
HE-3 Total Natural Gas Emissions(Ibtyr) 1041.48
HE-3 No.6 Total Fuel Oil Emissions(Ibtyr) 0.00
Total HE-3 Emissions(lb/yr) 1041.48
HE-4 Total Natural Gas Emissions(Ibtyr) 16451.09 „(1
HE-4 No.6 Total Fuel Oil Emissions(Ibtyr) 0.00 U
Total HE-4 Emissions(Ibtyr) 16451.09 `
HE-5 Total Natural Gas Emissions(Ibtyr) 14946.66
HE-5 No.6 Total Fuel Oil Emissions(lb/yr) 2.23
Total HE-5 Emissions(Ib/yr) 14948.89
2013%S in No.6 Fuel Oil(average) 2,10
6/24/2014 AEI Calculations 2013

ES06,ES07,ES08-Dowtherrn Heaters(HE-3,HE-4,HE-5)
Emission Factor Emission Factor Emissions From Emissions From Total 2012 Actual Emissions Total 2012 Actual
HE-5 Natural HE-6 Natural
Pollutant for No.6 Fuel for Natural Gas From Dowtherm Heaters Emissions From
Oil(lb/gal) 0blmmcf) Gas ONLY Gas ONLY i (Iblyr) Dowtherm Heaters(tonlyr)
(Iblyr) (tonlyr) NG Emissi
Criteria Air Pollutants -
Total PM 2.27E-02 7.6 519.94 026i 1,128.55 a 56 0.00
Filterable PM-10 1.95E-02 7.6 519.94 0.291 1,128.54 0.56 0.00
Filterable PM-2.5 1.27E-02 7.6 519,94 026' 1,128.50 0.56 0.00
NOx 5.50E-02 100 6.841.30 3,Q_ 14 848.18 7.42 0.00
CO 5.00E-03 84 5,746.69 2,87_ 12 472.26 6.24 0.00
S02 3.30E-01 0.6 4105 002 90.74 0.05 0.00
VOC 2.80E-04 5.5 376,27 0.19 816.64 0.41 0.00
Total HAP 1.83E-04 1.89 129.20 0.06 28040 0.14 0.00
Largest HAP 8 45E-05 1 80 123A4 0.06 267 261 0 13 0.00
Greenhouse Gas GHG Emissions
CO2 _ 2.50E+01 120000 8.209,560 4.105 17,817.605 8,909 0.06
CH4 1.00E-03 2.30 157.35 0.08 341 511 0.17 0.00
N20 1 1 OE-04 2 20 150.51 0,081 326 65 1 0.16 0.00
ToxictHazardous Air Pollutants
Antimony 525E-06 0 0.00E+00 _ 0.00E+00 2.63E-05 1 31E 08 0.0000 0.00E+00
Arsenic 1.32E-06 2.00E-04 i.37E-02 6.84E-08 2.97E-02 1.49E-05 0.0000 2.97E-02
Benzene 2.14E-07 2.10E-03 1,44E-01 7.18E-05 3.12E-01 1.56E-04 0,0000 3.12E-01
Beryllium 2.78E-08 1.20E-05 8 21 E-04 4.10E-07 1.78E-03 8.91E-07 0.0000 1.78E-03
Cadmium 3.98E-07 1.10E-03 7 53E-02 3,76E-05 1.63E-01 8.17E-05 0.0000 1.63E-01
Chromium 8.45E-07 1.40E-03 9.58E-02 4.79E-05 2.08E-01 1.04E-04 0.0000 2.08E-01
Chromium VI 2.48E-07 0 0.00E+00 0.00E+00 1.24E-06 6.20E-10 0.0000 0.00E+00
Cobalt 6.02E-06 8.40E-05 5.75E-03 _ 2.87E-06 1.25E-02 6.25E-06 0,0000 1.25E-02
Dichlorobenzene-1,4 0 1.20E-03 8.21E-02 4,10E-05 1.78E-01 8.91E-05 0.0000 1.78E-01
Eth(benzene 6.36E-08 0 _ OAOE+00 000E+00 3.18E-07 1.59E-10 0.0000 0.00E+00
Fluoride 3.73E-05 0 0.00E+00 6.09E+00 1.87E-04 9.33E-08 0.0002 0.00E+00
Formaldehyde 3.30E-05 7.50E-02 5.13E+00 2.57E-03 1.11E+01 5.57E-03 0.0002 1.11E+01
Hexane 0 1.8 1.23E+02 6.16E-02 2.67E+02 1.34E-01 0.0000 2.67E+02
Lead 1.51E-06 5.00E-04 3.42E-02 1.71E-05 7.42E-02 3.71E-05 0.0000 7.42E-02
Manganese 3.00E-06 3.80E-04 2.60E-02 _ _ 1.30E-05 5.64E-02 2.82E-05 0.0000 5.64E-02
Mercury _1.13E-07 2.60E-04 't78E-02 8.89E-06 3.86E-02 1.93E-05 0.0000 3.86E-02
Methyl chloroform 1 1 1-Trichloroethane 2.36E-07 0 0.00E+00 0AOE-00 1.18E-06 5.90E-10 0.0000 0.00E+00
Naphthalene 1.13E-06 6.10E-04 4.17E-02 2-09E-05 9.06E-02 4.53E-05 0.0000 9.06E-02
Nickel 8.45E-05 2.10E-03 i.44E-01 7.18E-05 3.12E-01 1.56E-04 0.0004 3.12E-01
POM 1.20E-06 8.82E-05 603E:-03 -3.02E-06 1.31E-02 6.55E-06 0.0000 1.31E-02
Selenium 6.83E-07 2.40E-05 1.64E-03 8.21E-07 3.57E-03 1.78E-06 0.0000 3.56E-03
Toluene 6.20E-06 3.40E-03 2.33E-01 1.15E-04 5.05E-01 2.52E-04 0.0000 5.05E-01
0-X lane 1.09E-07 0 0.00E+00 000E+00 5.45E-07 2.73E-10 0.0000 0.00E+00
2012
No.6 Fuel Oil Usage for HE-3(gaVyr) 0
No.6 Fuel Oil Usage for HE-4(gaVyr) 0
No.6 Fuel Oil Usage for HE-5(galtyr) 5
Used Oil Consumption for HE-5(gaVyr) 0
Natural Gas Usage for HE-3(mmcfyr) 4.767
Natural Gas Usage for HE4(mmcfyr) 75.299
Natural Gas Usage for HE-5(mmcfyr) 68.413 48 475
HE-3 Total Natural Gas Emissions(lb/yr) 1041.48
HE-3 No.6 Total Fuel Oil Emissions(lb/yr) 0.00
Total HE-3 Emissions(lb/yr) 1041.48
HE4 Total Natural Gas Emissions(Ibyr) 16451.09
HE4 No.6 Total Fuel Oil Emissions(Ibyr) 0.00 wq
Total HE-4 Emissions(Ibyr) 16451.09 U
HE-5 Total Natural Gas Emissions(lb/yr) 14946.66
HE-5 No,6 Total Fuel Oil Emissions(Ibyr) 2.23
Total HE-5 Emissions(Ibyr) 14948.89
2013%S in No.6 Fuel Oil(average) 2.10
6242014 AEI Calculations 2013

ES09 - Process Cooling Towers (TW-2 and TW-3)
Concentration in 2013 Total Actual Emissions Windage
Pollutant Cooling Water Drift Loss Evaporation Loss Loss
b Ib/hr Ib/ r Ib/hr Ib! r Ib/hr lbs! r tons/ r
1,4-Dioxane ` 5 2.20E-06 1.90E-02 8.24E-07 7.12E-03 3.02E-06 0.03 0.000
Antimony ** 76,600 3.37E-02 2.91 E+02 1.26E-02 1.09E+02 4.63E-02 399.89 0.200
Diethylene Glycol * 5,500 2.42E-03 2.09E+01 9.06E-04 7.83E+00 3.32E-03 28.71 0.014
Ethylene Glycol 46,300,000 2.03E+01 1.76E+05 7.63E+00 6.59E+04 2.80E+01 241,710.81 120.855
Toluene * 14 6.15E-06 5.32E-02 2.31 E-06 1.99E-02 8.46E-06 0.07 0.000
PM 0.05 399.89 0.200
VOc 27.98 241,739.62 120.870
**Annual Average EG in Cooling Water 4.63 % rg�yo
Cooling Tower Circulation Rate 3,620 gpm PM = PM10 = PM2.5
Cooling Tower Operating Hours 8,640 hr/yr
2013 Throughput 31,276,800 gal/yr
Cooling Water Density 8.43 lb/gal
Windage Rate 0.033 %
Drift Loss of Circulating Water 0.024 % 05 y
*Determined by analytical testing (see Summit Analytical Labs Report, Marley Process, 11/2/04)
**Based on historical data
3
C)
6/24/2014 AEI Calculations 2013
L
r,

ES10 - Spindraw Machines SM1 - SM 12
015 S- U
Pollutant Emission Rate Total Operating Actual Emissions u ,
Ib/hr Hours yr ton yr
Total PM 1.98 8,496 16,822.1 8.411 rz-5 i G 3
GS (C A . Z
PM = PM10 = PM2.5
Average Emission 1.98 Ib/hr PM
Rate (lb/hr) from
Operating hours per year Z 5
based on Polymer operating
hours: 8,496 hr/yr IZ S �d `
IDS �03° �
Emissions testing was performed by ETG, Inc. on May 24 -25, 2004 after filter change, the r $ J 13' Y
average emission rate was 1.65 lb/hr. Previous test was conducted on September 25, 5 1V
2003 was prior to filter change and the result was 2.31 lb/hr.
�-
Since annual source testing is no longer required for this source, an average of these two
most recent tests were used (1.98 Ib/hr).
6/24/2014 AEI Calculations 2013

ES11 - Emergency Generator
Input Specifications: V)
Max Design Capacity (kW) 400 v f-�►
Run time obtained from Utilities log (hrs/yr) 26
Conversion Factor(Btu/hp-hr) 2,544.4
Heat Content(Btu/gal) 140,000
Conversion Factor(hp/kW) 1.341
Annual Fuel Usage (gal/yr) 253.47
Note :Generator is typically tested every Sunday night for approximately 30 minutes,
but may have more run time.
Annual Throughput 13,946.4 (hp-hr/yr)
Pollutant Emission Factor Actual Emissions
Ib/h -hr Ib! r ton! r
Criteria Pollutants
PM 2.20E-03 30.68 1.53E-02
PM-10 2.20E-03 30.68 1.53E-02
PM-2.5 2.20E-03 30.68 1.53E-02
NOx 3.10E-02 432.34 2.16E-01
TOC, Total 2.51 E-03 35.06 1.75E-02
CO 6.68E-03 93.16 4.66E-02
Sox 2.05E-03 28.59 1.43E-02
Total HAP 2.71 E-05 0.38 1.89E-04
Largest HAP 8.26E-06 0.12 5.76E-05
Greenhouse Gas (GHG) Emissions
CO2 1.15E+00 16,038 8.02
CH4 ----- ----- -----
N2O ----- ----- -----
Toxic/Hazardous Air Pollutants
Acetaldehyde 5.37E-06 0.075 3.74E-05
Acrolien 6.48E-07 0.009 4.52E-06
Benzene 6.53E-06 0.091 4.55E-05
1,3-Butadiene 2.74E-07 0.004 1.91E-06
Formaldehyde 8.26E-06 0.115 5.76E-05
Naphthalene 5.94E-07 0.008 4.14E-06
POM 5.82E-07 0.008 4.06E-06
Toluene 2.86E-06 0.040 2.00E-05
Xylenes 2.00E-06 0.028 1.39E-05
Total VOC 1 2.71 E-05 3.78E-01 I 1.89E-04
6/24/2014 AEI Calculations 2013
I Z

ES16, ES17, ES18, ES19 -Storage/Holding Tanks (VT-20, VT-19, VT-34, VT-78)
Tank Data
-rvr,tq Tt�3y
Emission Source ID ES16 ES17 ES18 ES19
Tank ID VT-20 VT-19 -34 VT-78
Chemical Stored Spent EG Virgin EG Virgin EG DIPA
Concentration% 68.2 100 100 100
Dimensions
Type Vertical Vertical Vertical Vertical
Shell Height(ft) 30.25 30.25 30.25 14
Shell Diameter(ft) 34 34 34 12
Maximum Liquid Height(ft) 30.25 30.25 30.25 14
Average Liquid Height(ft) 15.125 15.125 15.125 7
Working Volume(gal) 205,449 205,449 205,449 11,844
Turnovers per Year 0.169 8.653 8.653 1.960
Is Tank Heated No No No No
Shell Characteristics
Shell Color/Shade White Gray/Med Gray/Med AI/Diffuse
Shell Condition Good Good Good Good
Roof Characteristics
Color/Shade White Gray/Med Gray/Med AI/Diffuse
Condition Good Good Good Good
Type Dome Dome Dome Dome
Height(ft) 4.65 4.65 4.65 1.33
Radius (ft) 17 17 17 9
Breather Vent Settings
Vacuum Setting (psig) 0 -0.03 -0.03 -0.03
Pressure Setting (psi ) 1 0 0.03 0.03 0.03
Liquid Physical Properties
Density
MV11, @ 60F, 'Antoine Coefficients
Component CASRN Ib/Ibmol lb/gal A B C
Ethylene Glycol (EG) 107-21-1 62.069 9.28 20.2501 6022.18 -28.25
Diisopropylamine(DIPA) 108-18-9 101.193 5.98 15.6973 2807.94 -51.20
Water H2O) 7732-18-51 18.015 8.34 18.3036 3816.44 -46.13
"Antoine Equation: In P=A-B/(C+T)
P, mm Hg
T, K
6/24/2014 AEI Calculations 2013

Temperature Vapor Pressure, psia
F K EG DIPA H2O
40 277.59 0.000391 0.521362 0.118792
50 283.15 0.000661 0.701704 0.174836
60 288.71 0.001095 0.931393 0.252804
70 294.26 0.001774 1.220367 0.359556
80 299.82 0.002819 1.579803 0.503557
90 305.37 0.004397 2.022154 0.695123
100 1 310.93 0.006740 2.561175 0.946671
"The Properties of Gases and Liquids, Reid, Prausnitz, Sherwood,Third Edition
Output from TANKS Software (Version 4.0.9d)
ES16 -Spent Ethylene Glycol Storage Tank(VT-20)
Working Breathing
Components Loss Loss Total Emissions /
Ib/ r Ib/ r Ib! r ton/ r S
EG 0.02 1.19 1.21 0.00061
Total VOC 0.00061
ES17-Virgin Ethylene Glycol Tank(VT-19)
Working Breathing
Components Loss Loss Total Emissions
Ib/ r Ib! r Ib/ r ton/ r
EG 4.87 8.04 12.91 0.00646
Total VOC 0.00646
ES18-Virgin Ethylene Glycol Tank(VT-34) �sj � ' 1 ✓T ��
Working Breathing
7✓7 3Y
Components Loss Loss Total Emissions
Ib/ r Ib! r Ib! r ton/ r
EG 4 87 8.04 12.91 0.00646
Total VOC 0.00646 _
ES19-DIPA Holding Tank(VT-78)
Working Breathing
Components Loss Loss Total Emissions l (7
Ib/ r Ibl r Ib/ r tonl r
DIPA 63.98 506.25 570.22 0.28511 J 1
Total VOC 0.28511
6/24/2014 AEI Calculations 2013
� y

ES20 - Emergency Diesel Fire Pumps (CP-28 and CP-593)
Emission Actual Emissions
Pollutant Factor CP-28 CP-593 Total
Ib/hp-hr Iblyr ton/yr Ib/yr ton/yr lb/yr ton/yr
Criteria Air Pollutants
PM 2.20E-03 17.23 8.61 E-03 13.44 6.72E-03 30.67 1.53E-02
PM-10 2.20E-03 17.23 8.61 E-03 13.44 6.72E-03 30.67 1.53E-02
PM-2.5 2.20E-03 17.23 8.61 E-03 13.44 6.72E-03 30.67 1.53E-02
NOx 3.10E-02 242.73 1.21 E-01 189.41 9.47E-02 432.14 2.16E-01
TOC, Total 2.51 E-03 19.69 9.84E-03 15.36 7.68E-03 35.05 1.75E-02
CO 6.68E-03 52.30 2.62E-02 40.81 2.04E-02 93.12 4.66E-02
sox 2.05E-03 16.05 8.03E-03 12.53 6.26E-03 28.58 1.43E-02
Total HAP 2.71 E-05 0.21 1.06E-04 0.17 8.28E-05 0.38 1.89E-04
Largest HAP 8.26E-06 0.06 3.23E-05 0.05 2.52E-05 0.12 5.76E-05
Greenhouse Gas (GHG) Emissions
CO2 1.15E+00 9,005 4.50 7,027 3.51 167031 8.02
CH4 ----- ----- ----- ----- ----- ----- -----
N20 ----- ----- ----- ----- ----- ----- -----
Toxic/Hazardous Air Pollutants
Acetaldehyde 5.37E-06 0.042 2.10E-05 0.033 1.64E-05 0.075 3.74E-05
Acrolien 6.48E-07 0.005 2.53E-06 0.004 1.98E-06 0.009 4.51 E-06
Benzene 6.53E-06 0.051 2.56E-05 0.040 2.00E-05 0.091 4.55E-05
1,3-Butadiene 2.74E-07 0.002 1.07E-06 0.002 8.36E-07 0.004 1.91E-06
Formaldehyde 8.26E-06 0.065 3.23E-05 0.050 2.52E-05 0.115 5.76E-05
Naphthalene 5.94E-07 0.005 2.32E-06 0.004 1.81E-06 0.008 4.14E-06
POM 5.82E-07 0.005 2.28E-06 0.004 1.78E-06 0.008 4.06E-06
Toluene 2.86E-06 0.022 1.12E-05 0.017 8.75E-06 0.040 2.00E-05
Xylenes 2.00E-06 0.016 7.81 E-06 0.012 6.09E-06 0.028 1.39E-05
Total V C 2.71 E-05 0.212 1.06E-04 0.166 8.28E-05 0.378 1.89E24
CP-28 Output 290 hp
Annual Operating hours 27 hr/yr
Annual Throughput 7,830 hp-hr/yr
CP-593 Output 235 hp OS / 7 7-
Annual Operating hours 26 hr/yr
Annual Throughput 6,110 hp-hr/yr Z C1<7- S q 3
-Z
(D
6/24/2014 AEI Calculations 2013
lj

ES21.ES22-Ethylene Glycol Recycle Feed Tanks MT-121 n �.; S 2- 1
Shell Length 9 ft
Shell Diameter 5 ft
Tank Capacities 176.7 cf each
1,321.9 gal each
Average Free Space Volume 35 cf each
Air Changes 10 Mr
Air Sweep Rate 350.0 cfh
Gas Constant 999 mmHg-cf/Ibmol-K
HT-126A
Alan III Production Hours 8,496 hr/yr
vol of Free
Temp,°C P,mmHg Air Flow cfh %Sat I Space,cf I n,Ib mols VR2,cfh
40 760 350.00 50 1 35.0 0.09 355.42
`Antoine Coefficients
Co m onent Wt.°!o__ MW TbAbinol Ibmot/lbri X,ri A B C VP,mmHg X*VP ni Y ER Ib/hr Ibl r ton/ r
Acetaldehyde 0.00 44,054 0.00E+00 0.00 16.2481 2465.15 -37.15 1504.77 0.00E+00 0 00E+00 0.000 0.00 0.000
Ethylene Glycol 82.88 62.069 1.34E+00 58.42 20.2501 6022.18 -28.25 0.41 1.20E-01 1 58E-04 0.008 72.03 0.036
Water 13.91 18.015 7.72E-01 33.78 18.3036 3816.44 -46.13 55.20 9.32E+00 1.23E-02 0.191 1,621.23 0.811
Inert 3.21 18.015 1.78E-01 7.80 18.3036 3816.44 -46.13 55.20 2.15E+00 2.83E-03 0.044 374.13 0.187
Total 100.00 2.29E+00 100.00 1.16E+01 1.53E-02 0,243
HT-126B
Alan IV Production Hours: 0 hr/yr
Volof Free
Temp,°C P.mm' I Hg Air Flow,cfh l Sat I Space,cf I n,lb mols VR2,cfh
40 760 350.00 50 35.0 0.09 363.19
*Antoine Coefficients
Component I Wt.% ji Ib/Ibmoj Ibmol/lbr l X,mol% A B C I VP mmHg X*VP,mmH Y I ER,Ib/hr I Ib/ r tonl r
Acetaldehyde 0.00 44.054 0.00E+00 0.00 16.2481 2465.15 -37.15 1504,77 0.00E+00 0.00E+00 0.000 0.00 0.000
Ethylene Glycol 0.00 62.069 0.00E+00 0.00 20.2501 6022.18 -28.25 0.41 0.00E+00 0.00E+00 0.000 0.00 0.000
Water 0.00 18.015 0.00E+00 0.00 18.3036 3816.44 -46.13 55.20 0.00E+00 0.00E+00 0.000 0.00 0.000
Inert 100.00 18.015 5.55E+00 100.00 18.3036 3816.44 -46.13 55.20 2.76E+01 3.63E-02 0.577 0.00 0.000
Total 100.00 5.55E+00 100.00 2.76E+01 3.63E-02 0.577
*The Properties of Gases and Liquids,Reid,Prausnitz,Sherwood,Third Edition Totals for HT-126A+HT126B Ib/ r ton/yr
**VR2 takes in to account the N2 sweep in the vessel. See ref.Document VOC Emissions from Batch Chemical Processes. Acetaldehyde 0.00 0.000
Ethylene Glycol 72.03 0.036
VR2,gal/hr=Air Flow(cfh)x P,mmHg/[P-(Sum X*VP)I.mmHg Total VOC 72.03 0.036
6/24/2014 AEI Calculations 2013
�T

ES26-Ethylene Glycol Recycle Tank(HT-11)
Shell Length 40 ft
Shell Diameter 10 ft
Tank Capacity 3,141.6 cf
23,500.7 gal
Average Free Space Volume 8,297.0 gal
Air Sweep Rate 120.0 cfh
Gas Constant 999 mmHg-cf/lbmol-K
Volof Free
Temp,°C P,mmHg Air Flow,cfh %Sat I Space,cf I n,lb mols I VR2,cfh
65 760 120.00 50 2,032.4 4.57 123.83
*Antoine Coefficients
Component I Wt.% IM,lb/lbirnollbrnol/lbirnatil X mol%a I A B I C I VP mmHg X*VP,mmHcj Y I ER,Whir I lbt r I tont r
Acetaldehyde 0.00394 44.054 8.94E-05 0.00 16.2481 2465.15 -37.15 3159.70 7.27E-02 9.57E-05 0.001 10.29 0.005
Ethylene Glycol 91.58 62.069 1.48E+00 75.95 20.2501 6022.18 -28.25 2.26 8.60E-01 1 13E-03 0,020 171.40 0.086
Water 5.71 18.015 3.17E-01 16.32 18.3036 3816.44 -46.13 187.63 1.53E+01 2.01E-02 0.101 885.44 0.443
Inert 2.71 18.015 1.50E-01 7.73 18.3036 3816.44 -4613 187.63 7.25E+00 9.54E-03 0.048 419.62 0.210
Total 100.00 1 94E+00 100.00 2.35E+01 3 09E-02 0.170
*The Properties of Gases and Liquids,Reid,Prausnitz,Sherwood,Third Edition Total for HT-11 Ibl r ton! r
**VR2 takes in to account the N2 sweep in the vessel. See ref.Document VOC Emissions from Batch Chemical Processes. Acetaldehyde 10.29 0 005
Ethylene Glycol 171.40 0.086
VR2,gal/hr=Air Flow(cfh)x P,mmHg/[P-(Sum X*VP)),mmHg Total VOC 181.69 0 091
;2- 2- 7 z 3
Mr
OC
6/24/2014 AEI Calculations 2013

ES27,ES28-Steam Super Heaters(HE-553 and HE-554)
012
Emission Factor for Emission Factor Total Emissions Total Emissions Total Emissions Total s from
Total s from
n /^%d/a ,�Q L
Total Emissions Emissions from Emissions from �//tl �(,�(�1�r /tom
Pollutant Natural Ga for Propane from HE 553 from HE 553 from HE 554
from HE 554(Iblyr) Steam Super- Steam Super-
Immscf) (ICrf00U-W (lb/yr) (ton/yr) (ton/yr)
heaters(Ib/yr) heaters(tonlyr)
i err °'a, e�, -* .°,
Total PM 7.6 0.60 87.28 0.04 87.28 0.04 174.56 0,09 �(..
Filterable PM-10 7.6 0.60 87.28 0.04 87.28 0,04 174.56 0.09
Filterable PM-2.5 7.6 0.60 87.28 0.04 8Z28 0,04 174.56 0,09
NOx 100 19.00 1148A0 0.57 1148,40 0.57 2296,80 1.15
CO 84 3.20 964.66 0.48 964.66 0.48 1929.31 0.96 J I
SO2 0.6 0.21 6.89 0.00 6.89 0.00 13,78 0,01
VOC 5.5 0.50 63.16 0.03 63.16 0.03 126.32 0.06
Total HAP 1 89 N/A 21 69 1 0,01 21.69 0 01 43 37 0 02
Largest �
CO2 120,000 12,500 1,378,080 1 689 1,378,080 689 2,756,160 1,378
CH4 2.3 0.20 26,41 1 0,01 26.41 0.01 52.83 0,03
2012
Emission Factor for Total Emissions Total Emissions Total Emissions Total Total
Pollutant Natural Gas from HE-553 from HE-553 from HE-554 Total Emissions Emissionss f frrom Emissionss from
(lb/mmscf) (Ib/yr) (ton/yr) (Ib/yr) from HE-554(ton/yr) Steam Super- Steam Super-
heaters(Ib/yr) heaters(tonlyr)
TO)WHU&Ow r.... .,a
Antimony N/A NIA N/A N/A N/A N/A N/A
Arsenic 2.00E-04 0.002 1.148E-06 0.002 1148E-06 0.005 2.297E-06
Benzene 2.10E-03 0.024 1.206E-05 0.024 1.206E-05 0.048 2.412E-05
Beryllium 1.20E-05 0,000 6.890E-08 0.000 6.890E-08 0,000 1.378E-07
Cadmium 1.10E-03 0.013 6.316E-06 0.013 6.316E-06 0.025 1.263E-05
Chromium 1.40E-03 0.016 8.039E-06 0.016 8.039E-06 0.032 1.608E-05
Chromium VI N/A N/A N/A N/A N/A N/A N/A
Cobalt 8.40E-05 0.001 4.823E-07 0,001 4.823E-07 0,002 9.647E-07
Dichlorobenzene-1,4 1.20E-03 0.014 6.890E-06 0,014 6.890E-06 0.028 1.378E-05
Eth (benzene N/A N/A N/A N/A N/A N/A N/A
Fluoride N/A N/A N/A N/A N/A N/A N/A
Formaldehyde 7.50E-02 0.861 4.307E-04 0.861 4.307E-04 1.723 8.613E-04
Hexane 1.80E+00 20.671 1.034E-02 20.671 1.034E-02 41.342 2.067E-02
Lead 5.00E-04 0.006 2.871E-06 0.006 2.871E-06 0.011 5.742E-06
Manganese 3.80E-04 0.004 2.182E-06 0.004 2.182E-06 0,009 4.364E-06
Mercury 2.60E-04 0.003 1.493E-06 0.003 1493E-06 0.006 2.986E-06
Methyl chloroform 1,1,1-Trichloroeth N/A N/A N/A N/A N/A N/A N/A
Naphthalene 6.10E-04 0.007 3.503E-06 0.007 3.503E-06 0.014 7.005E-06
Nickel 2.10E-03 0.024 1.206E-05 0.024 1.206E-05 0 048 2.412E-05
POM 8.82E-05 0,001 5.064E-07 0.001 5.064E-07 0.002 1.013E-06
Selenium 2.40E-05 0.000 1.378E-07 0.000 1.378E-07 0.001 2.756E-07
Toluene 3.40E-03 0.039 1.952E-05 0.039 1,952E-05 0.078 3.905E-05
X lene NIA N/A
6/24/2014 AEI Calculations 2013

C(�4.243 cf(gas)/gal(liquid) SUPERHEATER HE-553 SUPERHEATER HE-564
19 Ib/cf @ 70F) 2012 Operating Hrs: 0 hrs 2012 Operating Hrs: 0 hrs
Maximum Firing Rate: 10 MMbtu/hr Maximum Firing Rate: 10 MMblu/hr Nv T V f0i2QATZ
2012 FUEL USAGE AND HEAT INPUT 2012 FUEL USAGE AND HEAT INPUT f
Natural Gas: 11.484 MMcf/yr Natural Gas: 11.484 MMcf/yr
Heat Content: 1020 Btu/cf Heat Content: 1020 Btu/cf
Propane: 0 MMcf/yr Propane: 0 MMcf/yr �5 /
0.000 1000 gal/yr 0.000 1000 gal/yr
Heat Content: 91,500 Btu/gal Heat Content: 91,500 Btu/gal
Propane Sulfur Content
Sulfur content in propane calculated according to the maximum ethyl mercaptan content(50 ppm)
as provided in suppliers MSDS.
S + C2H6 -> C2H6S
50 lb CAS x 1 mole C21-16S x 1 mole S x 32 lb S
10 lbw Propane 62 lb CzHeS 1 mole C2H6S 1 mole S
25.8 lb S
106 Propane
_- 26 ppm S
_- 0.0026 wt.%S in Propane
25.8 lb S x 7,000 grains S x 11.9 lb Propane
10 lb� lb S 100 ft3 Propane
2.1497 grains S
100 ft3 Propane
Natural Gas POM Emission Factor Calculation(from AP-
42)
2-Methylnaphthalene 2.40E-05
3-Methylchloranthrene 1.80E-06
7,12-Dimethylbenz(a)anthracene 1.60E-05
Acenaphthene 1.80E-06
Acenaphthylene 1.80E-06
Anthracene 2.40E-06
Benz(a)anthracene 1.80E-06
Benzo(a)pyrene 1.20E-06
Benzo(b)fluoranthene 1.80E-06
Benzo(g,h,i)perylene 1.20E-06
Benzo(k)fluoranthene 1.80E-06
Chrysene 1.80E-06
Dibenzo(a,h)anthracene 1.20E-06
Fluoranthene 3.00E-06
Fluorene 2.80E-06
Indeno(1,2,3-cd)pyrene 1.80E-06
Phenanathrene 1.70E-05
Pyrene 5.00E-06
TOTAL POM 8.82E-05
6/24/2014 AEI Calculations 2013

ES29 - Ethylene Glycol Recovery Tank (HT-10)
Shell Length 17 ft
Shell Diameter 10 ft
Tank Capacity 1335.2 cf
9,987.8 gal
Average Free Space Volume 3,500.0 gal
Air Sweep Rate 120.0 cfh
Gas Constant 999 mmHg-cf/Ibmol-K
Vol of Free
Temp,°C P,mmHg �ir Flow,cf %Sat Space,cf n,lb mols VR2,cfh
60 760 120.00 50 867 1.98 130.68
`Antoine Coefficients
Component I Wt.% MW,Ib/lbmoPbmol1lbmatj X,mol% I A I B I C I VP,mmH *VP,mmHd Y I ER,Iblhr ib/ r ton/ r
Acetaldehyde 0 00 44.054 0.00E+00 0.00 16.2481 2465 15 -37.15 2751.47 0.00E+00 0.00E+00 0 000 0.00 0.000
Ethylene Glycol 41.44 62.069 6.68E-01 17.04 20.2501 6022.18 -28.25 1.65 1.40E-01 1.85E-04 0.003 29.95 0.015
Water 6.96 18.015 3.86E-01 9.85 18.3036 3816.44 -46.13 149.43 7.36E+00 9.69E-03 0.052 456.17 0.228
Inert 51.61 18.015 2.86E+00 73.11 18.3036 3816.44 -46.13 149.43 5.46E+01 7.19E-02 0.386 3384.70 1.692
Total 100.00 3.92E+00 100.00 6.21 E+01 8.17E-02 0.442
*The Properties of Gases and Liquids, Reid, Prausnitz,Sherwood,Third Edition Total for HT-10 Ib/yr ton/yr
**VR2 takes in to account the N2 sweep in the vessel. See ref. Document VOC Emissions from Batch Chemical Processes. Acetaldehyde 0.00 0.000
Ethylene Glycol 29.95 0.015
VR2,gal/hr=Air Flow(cfh)x P,mmHg/[P-(Sum X*VP)],mmHg Total VOC 29.95 0.015 /
2
6/24/2014 AEI Calculations 2013

ES30 -Distillation Column Bottoms Purified EG Tank(HT-25) -S
Tank Data
Emission Source ID ES30
Tank ID HT-25
Chemical Stored Purif EG
Concentration% 99
Dimensions
Type Horizontal
Shell Length(ft) 50
Shell Diameter(ft) 10.37
Working Volume(gal) 31,590 _
Turnovers per Year 0.000 +7
s Tank Heated No
Is Tank Underground No
Shell Characteristics
Shell Color/Shade lumin/Dill
Shell Condition Good
Breather Vent Settings
Vacuum Setting(psig) -0.25
Pressure Setting si 0.75
Liquid Physical Properties
Density
MW, @ 60F; "Antoine Coefficients
Component CASRN Ib/Ibmol Ibl al A B C
Ethylene Glycol(EG) 107-21-1 62.069 9.28 202501 6022.18 -28.25
Water H2O 7732-18-5 18.015 8.34 18.3036 3816.44 -46.13
'Antoine Equation: In P=A-B/(C+T)
P, mm Hg
T,K
Temperature Vapor Pressure, psia
F K EG H2O
40 277.59 0.000391 0.118792
50 283.15 0.000661 0.174836
60 288.71 0.001095 0.252804
70 294.26 0.001774 0.359556
80 299.82 0.002819 0.503557
90 305.37 0.004397 0.695123
100 310.93 0.006740 0.946671
'The Properties of Gases and Liquids, Reid,Prausnitz,Sherwood,Third Edition
Output from TANKS Software(Version 4.0.9d)
ES30-Purified Ethylene Glycol Tank(HT-25)
Working Breathing
Components Loss Loss Total Emissions
lb! r Ib! r lb/ r ton/ r
EG 0.00 0.20 0.20 0.00010
Total VOC 0.00010
6/24/2014 AEI Calculations 2013
�� I

ES32,ES33-Pyrolysis Furnaces(I-OV-1&I-OV-2)
Emission Factor Total 2013 Emissions
Emission Factor for Total Emissions from I- Total Emissions Total Emissions from I- Total Emissions Total 2013 Emissions from
Pollutant for Natural Gas Propane(lb/1000 gal) OV-1(lb/yr) from I-OV-1(ton/yr) OV-2(lb/yr) from I-OV-2(ton/yr) from Pyrolysis Pyrolysis Furnaces(ton/yr)
(Ib7RIMc Furnaces(lb/yr)
x
Total PM 7.6 0.60 2.76E+00 1.38E-03 2.76E+00 1 38E-03 5.51 E+00 2.76E-03
Filterable PM-10 7.6 0.60 2.76E+00 1.38E-03 2.76E+00 1.38E-03 5.51E+00 2.76E-03
Filterable PM-2.5 7.6 0.60 2.76E+00 1.38E-03 2.76E+00 1.38E-03 5.51E+00 2.76E-03
NOx 100 19.00 3.63E+01 1.81 E-02 3.63E+01 1.81 E-02 7,25E+01 3.63E-02
CO 84 3.20 3.05E+01 1.52E-02 3.05E+01 1.52E-02 6.09E+01 3.05E-02
S02 0.6 0.21 2.18E-01 1.09E-04 2.18E-01 1.09E-04 4.35E-01 2.18E-04
VOC 5.5 0.50 1.99E+00 9.97E-04 1.99E+00 9.97E-04 3.99E+00 1.99E-03
Total HAP 1.89 N/A 6.85E-01 3.42E-04 6.85E-01 3.42E-04 1.37E+00 6.85E-04
Largest 6.53E-01 3.26E-04 6.53E-01 3.26E-04 1.31E+00 6.53E-04
CO2 120,000 12,500 43,500 21.75 43,500 21.75 87.000 43,50
CH4 2.3 0.20 8.34E-01 4.17E-04 8.34E-01 4.17E-04 1.67E+00 8.34E-04
7.98E-01 3.99E-04 7.98E-01 3.99E-04 1.60E+00 7.98E-04
�.
e.,v
7AX1 4, ale 7„z,>;
Antimony N/A N/A N/A N/A N/A N/A N/A N/A
Arsenic 2.00E-04 N/A 7.25E-05 3.63E-08 7.25E-05 3.63E-08 1.45E-04 7.25E-08
Benzene 2.10E-03 N/A 7.61E-04 3.81E-07 7.61E-04 3.81E-07 1.52E-03 7.61E-07
Beryllium 1.20E-05 N/A 4.35E-06 2.18E-09 4.35E-06 2.18E-09 8.70E-06 4,35E-09
Cadmium 1.10E-03 N/A 3.99E-04 1.99E-07 3.99E-04 1.99E-07 7.98E-04 3.99E-07
Chromium 1.40E-03 N/A 5.08E-04 2.54E-07 5.08E-04 2.54E-07 1.02E-03 5.08E-07
Chromium VI N/A N/A N/A N/A N/A N/A N/A N/A
Cobalt 8.40E-05 N/A 3.05E-05 1.52E-08 3.05E-05 1.52E-08 6.09E-05 3.05E-08
Dichlorobenzene-1,4 1.20E-03 N/A 4.35E-04 2.18E-07 4.35E-04 2.18E-07 8.70E-04 4.35E-07
Eth (benzene N/A N/A N/A N/A N/A N/A N/A N/A
Fluoride N/A N/A N/A N/A N/A N/A N/A N/A
Formaldehyde 7.50E-02 N/A 2.72E-02 1.36E-05 2.72E-02 1.36E-05 5.44E-02 2.72E-05
Hexane 1.80E+00 N/A 6.53E-01 3.26E-04 6.53E-01 3.26E-04 1.31 E+00 6.53E-04
Lead 5.00E-04 N/A 1.81E-04 9.06E-08 1.81E-04 9.06E-08 3.63E-04 1,81E-07
Manganese 3.80E-04 N/A 1.38E-04 6.89E-08 1.38E-04 6.89E-08 2.76E-04 1.38E-07
Mercury 2.60E-04 N/A 9.43E-05 4.71E-08 9.43E-05 4.71E-08 1.89E-04 9,43E-08
Methyl chloroform 1,1,1-Trichloroeth N/A N/A N/A N/A N/A N/A N/A N/A
Naphthalene 6.10E-04 N/A 2.21 E-04 1.11 E-07 2.21 E-04 1,11 E-07 4.42E-04 2.21 E-07
Nickel 2.10E-03 N/A 7.61 E-04 3.81E-07 7.61 E-04 3.81E-07 1.52E-03 7.61 E-07
POM 8.82E-05 N/A 3.20E-05 1.60E-08 3.20E-05 1.60E-08 6.39E-05 3.20E-08
Selenium 2.40E-05 N/A 8.70E-06 4.35E-09 8.70E-06 4.35E-09 1.74E-05 8.70E-09
Toluene 3.40E-03 N/A 1.23E-03 6.16E-07 1.23E-03 6.16E-07 2.47E-03 1.23E-06
Xylene
Propane: 35.63 cf(gas)/gal(liquid) PYROLYSIS FURNACE I-OV-1 PYROLYSIS FURNACE I-OV-2
i6ii lMgal/0.119 Ib/cf @ 70F) 2013 Operating Firs(est.): D hrs 2013 Operating Hrs(est.): 0 hrs
Maximum Firing Rate: m u/hr Maximum Firing Rate: 19111CUMT15tu/hr
2013 FUEL USAGE AND HEAT INPUT 2013 FUEL USAGE AND HEAT INPUT
Natural Gas: 0.3625 MMcf/yr Natural Gas: 0,3625 MMcf/yr
Heat Content: 1020 Btu/cf Heat Content: 1020 Btu/cf
Propane: 0.0000 MMcf/yr Propane: 0.0000 MMcf/yr
0.0000 1000 gal/yr 0.0000 1000 gal/yr
Heat Content: 91,500 Btu/gal Heat Content: 91,500 Btu/gal
0 6/24/2014 / T V V - AEI Calculations 2013 1,
L i D V-Z,

F01 - Alan III Vessel APT-101A Draininq
*Basis: 37.00 lb EG/drum
*Based on 1992 emissions testing and estimation study (444 Ibs EG emitted per 12-55 gallon drums filled)
Emission Calculation: 14 total drums filled in 2013
F01 Air Emissions 0 �' y
Component Ibi r Iton/ r Ethylene Glycoll 518 0.26 ITF 0
Total VOC 1 518 0.26
F02 - Alan IV Vessel APTA01B Draining
*Basis: 37.00 lb EG/drum
*Based on 1992 emissions testing and estimation study (444 Ibs EG emitted per 12-55 gallon drums filled)
Emission Calculation: 0 total drums filled in 2013
Component F02 Air Emissions O S
Ib/ r tonl r
Ethylene Glycol 0 0.00 7Z /= d 2,
Total VOC 0 0.00
O
6/24/2014 AEI Calculations 2013

F03-Alan III Vessel APT-117A Flush Dumping Line
Basis
1. Emissions are estimated based on flash calculations
2. Vapor pressures are calculated using Antoine's equation
In P=A-(B/(C+T))
P,mm Hg
T,K
3. Flush(F)=Vapor(V)+Liquid(L)
4. Vapor mole fractions are calculated using the following equation:
Yi=(KixZi)/(((Ki-1)x(V/F))+1)
5. Trial and error was used to develop a(V/F)number so that the total vapor mole fraction(Yi)equals 1
2010 Basis
Total Amount Flushed 63,378 Ib/yr
Maximum Temperature 381 F
467.0 K
Total Pressure,Pt 760 mm Hg
Flash Calculations
Flush Total Molecular Liquid Liquid Vapor Vapor
Compo- Amount Moles Mole ..Antoine Coefficients Pressure, Mole Vapor Composition
Component sition Flushed Weight Flushed Fraction, Pvi Ki=PvilPt Fraction,
wt% Ibl r Ib/lbmol Ibmoll r Zi A B C mm Hg Yi Ib/lbmol wt%,
EG 5.00 3,169 62.069 51.054 0.1024 20.2501 6022.18 -28.25 265.37 0.35 0.0406 2.52 12�8
Polymer 90.00 57,040 210 271.620 0.5448 -- ----- ----- --- -----
Water 5.00 3,169 18.015 175.903 0.3528 18.3036 3816.44 -46.13 3,362.44 4.42 0.9556 17.21 87.22
TOTALS 100,00 63.378 498.578 1.0000 0.9962 1974 10000
V/F= 0.185
V= 1,172A9 Ibs/yr
Emission Calculations O
Component 2012 Emissions
bl r o v[
EG 149.88 0.075
Water 1,022.61 0.511 F O
/ 1 Total 1,172.49 0.586
�II
6/24/2014 AEI Calculations 2013

F04-Alan IV Vessel APT-117B Flush Dumping Line
Basis
1. Emissions are estimated based on flash calculations
2. Vapor pressures are calculated using Antoine's equation
In P=A-(B/(C+T))
P,mm Hg
T,K
3. Flush(F)=Vapor(V)+Liquid(L)
4. Vapor mole fractions are calculated using the following equation:
Yi=(Ki x Zi)/(((Ki-1)x(V/F))+1)
5. Trial and error was used to develop a(V/F)number so that the total vapor mole fraction(Yi)equals 1
2011 Basis
Total Amount Flushed 0 Ib/yr
Maximum Temperature 0 F
255.4 K
Total Pressure,Pt 760 mm Hg
Flash Calculations
Flush Total Mole Liquid Liquid Vapor Vapor
Component Compo- Amount Weight ecu ht lar Moles Mole Antoine Coefficients Pressure, Ki=Pvi/Pt Mole Vapor Composition
sition Flushed Flushed Fraction, Pvi Fraction,
wt% ib! r Iblibmoi ibmol! r._. ZI A B C mm H Yi b/ibmo wt to
EG 5.00 0 62.069 0.000 0.1024 20.2501 6022.18 -28.25 0.00 0.00 0.0000 000 0 71
Polymer 90.00 0 210 0.000 0.5448 ----- ----- ----- ----- ----- -----
Water 5.00 0 18.015 0.000 0.3528 18.3036 3816.44 -46.13 0.01 0.00 0.0000 0.00 99.29
TOTALS 100.00 0 0.000 1_0000 0.0000 0.00 100.00
V/F= 0.428
V= 0.00 Ibs/yr
Emission Calculations
Component 2012 Emissions
EG 0.0.00 0,000
Ok Water 0.00 0.000 r O
Total 0.00 0.000
6/24/2014 AEI Calculations 2013

F05 - Process Chillers
Basis
1. Emissions are estimated based on annual refrigerant consumption.
2. Consumption obtained from purchasing records and chiller inventory readings.
Amount
Refrigerant Chillers Consumed 2013 Air Emissions
Ib/yr Ib/yr ton/yr
Trichlorofluoromethane CFC-11 RG-4 600 600 0.3
Dichlorodifluoromethane CFC-12 RG-2, RG-3 0 0 0
Tetrafluoroethane HFC-134a RG-1 0 0 0
Total 600 600 0.3
-Tlzz
4
L �IT 67
O
6/24/2014 AEI Calculations 2013

F06 - Dowtherm Storage and Transfer System
Basis
Emissions are estimated based on annual Dowtherm A consumption that is tracked on a monthly
basis minus any heat transfer fluid that was collected in drums for recycle or collected on spill clean-up materials.
2013 Basis
2013 Dowtherm A consumption 2,615 gal/yr
No. of Recycle Drums(50 gal/drum) 13 drums/yr
Recycle Volume 650 gal/yr
No of Spill Cleanup Drums (4 gal/drum) 9 drums/yr
Spill Cleanup Volume 36 gal/yr
Dowtherm A Physical Properties
S.G. 1.056 @ 68 F (from Product Specification Sheet)
Density @ T 8.800 lb/gal
Emission Calculations
Total Dowtherm A Emitted 1,929 gal/yr
;. 16,975 Ib/yr
7
Biphenyl 27 4,583.3 2.292
Diphenyl Oxide 73 12,391.9 6.196
Total VOC 100 16,975.2 8.488
S
4
� 5 2-
r q 41
10
6/24/2014 AEI Calculations 2013

F07-Alan III Condenser Seal Pots
Basis
Emissions are estimated based on vapor-liquid equilibrium under air sweep conditions. / /JJ
Air sweeping rate was assumed to be 600 scfh. r C, Ai j �?•Z
n �
As a conservative assumption,100%of saturation in air after sweeping was assumed. vl ,,�yI -T ,� 5- ��T
TheWT-205A seal pot system is equipped with ethylene glycol(EG)jets instead of steam jets. Therefore,annual emissions
from OT-205A and MF-206A are based on the operation time that each was online during the calendar year. ^ P T �U
A P Zo(A
Seal Pot Operating Data
Actual Flow Rate Max.Temp Room
Seal Pots Reactors Temperature
m Ib/hr, C G
VT-205A/206A APT-201A 365 182,646 40 25
VT-305AI306A APT-301A 155 77,562 40 25 ✓T 3 ,1
VT-405AI406A APT-401A 200 100,080 40 25
VT-605/606 APT-601A 385 192,654 40 25
Seal Pot Configurations
Tank Size Liquid Height Max.Capacity Working
Seal Pots Volume
N(ft), ft aal aal
VT-205A/206A 4.0 1.8 3.0 2.75 161.6 148.1
VT-305AI306A 4.0 0.8 3.0 2.75 71.8 65.8
VT-405A/406A 4.0 0.8 3.0 2.75 71.8 65.8
VT-605/606 4.0 1.5 3.0 2.75 134.6 123.4
Test Data of Liquid Compositions
Seat Pots Ethylene Glycol Diethylene Glycol 1,4-Dioxane
m wit% ppm wt% m wte%
VT-205A 980,000 98.00 ---- -----
VT-206A 69,900 6.99 1,700 0.17 18.8 0.0019
VT-305A/306A 94,000 9.40 1.300 0.13 19.8 0.0020
VT-405A/406A 63,000 6.30 1,100 0.11 20.7 0.0021
VT-605/606 75,000 7.50 810 0.08 20.7 0.0021
"Compositions for all seal pots,with exception to VT-205A,determined through sampling and analysis in November 1994
"Ethylene glycol concentration in VT-205A is based on material balance.
�5 6/24/2014 AEI Calculations 2013

Emission Calculations
VT-205A
Tank Capacity 161.6 gal
Working Volume 148.1 gal
Air Sweep Rate 600.0 cfh
Operation Time 8,326.1 hr/yr
Gas Constant 999 mmHg-cf/Ibmol-K
Volof Free
Temp,'C P mmHg Air Flow,cfh %Sat I Space,cf n,Ib mols VR2,cfh
40 760 600 00 100 1 8 0 0044 603 18
Component Wt.% MW,Ib/Ibmol IbmoVlbmatI X m0l%o A B C VP mmN X P,mmHQ I Y I ER lb/hi lb! r
Ethylene Glycol 98.0000 62 069 1.58E+00 93.4305 20.2501 0022 18 -28 25 1 041 3.85E-01 5.06E-04 00460163, 383.16 0.192
Water 2.0000 18.015 1.11E-01 6.5695 18.3036 3816.44 -46.13 1 55.20 3.63E+00 4.77E-03 0.1259520 1048.69
Total 100.0000 1.69E+00 100.0000 4.01E+00 5.28E-03 0.172
VT-206A
Tank Capacity 161.6 gal
Working Volume 148.1 gal
Air Sweep Rate 600.0 cfh
Operation Time 169.9 hr/yr
Gas Constant 999 mmHg-cf/Ibmol-K
Volof Free
Temp,'C P mmH Aar Flow,cfh %n Sat. Space,cf n,lb mols VR2,cfh
40 760 600.00 100 1.8 0 0044 645.90
, C Y� ER 1bthr to'
Ethylene Glycol 6.9900 62.069 1.13E-01 2.1379 20.2501 6022 18 -28 25 0.41 8.80E-03 1.16E-05 0.0011276 0.19 0.000
Dieth lene Glycol 0.1700 106.122 1.60E-03 0.0304 17.0326 4122.52 -122.50 0.01 3.08E-06 4.06E-09 0.0000007 0.00 0.000
1,4-Dioxane 0.0019 88.107 2.13E-05 0.0004 16.1327 2966.88 62.15 74.62 3.02E-04 3.98E-07 0.0000550 0.01 0.000
Water 92.8381 18.015 5.15E+00 97.8313 18.3036 3816.44 -46.13 55.20 5.40E+01 7.11 E-02 2.0084710 341.28 0.171
Total 100.0000 1 5.27E+00 100.0000 5.40E+01 7.11 E-02 2.010
6/24/2014 AEI Calculations 2013

1
}
VT-305A/306A
Tank Capacity 71.8 gal
Working Volume 65.8 gal
Air Sweep Rate 600.0 cfh
Operation Time 8,496.0 hr/yr
Gas Constant 999 mmHg-cf/Ibmol-K
,h 1 trt i6>
40 760 600.00 100 0.8 0,0019 645.51
(Vfiryt lbXib ,ol"IbirtalflbfYibtl :.^X rriol°/a A_ _.,x .�,.B , ,. C.. VP,�ltinjHi X�/P;�Ym Ethylene Glycol 9.4000 62.069 1.51E-01 2.9267 20.2501 6022.18 -28.25 0.41 1.20E-02 1.58E-05 0.0015427 13.11 0.007
Dieth lene Glycol 0.1300 106.122 1.23E-03 0.0237 17.0326 4122.52 -122.50 0.01 2.40E-06 3.16E-09 0.0000005 0.00 0.000
1,4-Dioxane 0.0020 88.107 2.25E-05 0.0004 16.1327 2966.88 -62.15 74.62 3.24E-04 f7.O5E-02
-07 0.0000589 0.50 0.000
Water 90.4680 18.015 5.02E+00 97.0492 1..3036 3816.44 -46.13 55.20 5.36E+01 1.9912056 16917.28 8.459
Total 100.0000 5.17E+00 100.0000 5.36E+01 -02 1.993
VT-405A/406A
Tank Capacity 71.8 gal
Working Volume 65.8 gal
Air Sweep Rate 600.0 cfh
Operation Time 0.0 hr/yr
Gas Constant 999 mmHg-cf/Ibmol-K
re
LA
kv
TH},_^f H� ,_Atr.H law cfh', %la,Sat .. �n lb�tialsy VR2 Cflt v
40 760 600.00 100 0.8 0.0019 646.02
Ca>xi" ertt alo' ...s .. , Ad X* P`mitk Nt ° -MW;11>110 of`lbm G V .rri .
Ethylene Glycol 6.3000 62.069 1.01E-01 1.9160 20.2501 6022.18 -28.25 0.41 7.89E-03 1.04E-05 0.0010107 0.00 0.000
Dieth lene Glycol 0.1100 106.122 1.04E-03 0.0196 17.0326 4122.52 -122.50 0.01 1.98E-06 2.61 E-09 0.0000004 0.00 0.000
1,4-Dioxane 0.0021 88.107 2.35E-05 0.0004 16.1327 2966.88 -62.15 74.62 3.31E-04 4.35E-07 0.0000602 0.00 0.000
Water 93.5879 18.015 5.20E+00 98.0640 18.3036 3816.44 46.13 55.20 5.41 E+01 7.12E-02 2.0136129 0.00 0.000
Total 100.0000 5.30E+00 100.0000 5.41E+01 7.12E-02 2.015
6/24/2014 AEI Calculations 2013
O

VT-605/606
Tank Capacity 134.6 gal
Working Volume 123.4 gal
Air Sweep Rate 600.0 cfh
Operation Time 8,496.0 hr/yr
Gas Constant 999 mmHg-cf/Ibmol-K
VolOT Free
Temp,"C P mmHg Air Flow,cfh %Sat Space,cf n,lb mots VR2,cfh
40 760 600.00 100 1 5 0 0036 645 83
( Wt.% 1 Ibmol/Ibmatl I X,mol% A B C VP,mmHg X`VP,rnmFIg Y ER.Iblhr Ib/ r ton/ r
Ethylene Gl col 7.5000 62.069 1.21E-01 2.3009 20.2501 6022.18 -28.25 0.41 9.47E-03 1.25E-05 0.0012134 10.31 0.005
Dieth lene Glycol 0,0810 106.122 7.63E-04 0.0145 17.0326 4122.52 -122.50 0.01 1.47E-06 1.94E-09 0.0000003 0.00 0.000
1,4-Dioxane 0.0021 88.107 2.35E-05 0.0004 16.1327 2966.88 -62.15 74.62 3.34E-04 4.39E-07 0.0000607 0.52 0.000
Water 92.4169 18.015 5.13E+00 97.6841 18+3036 3816+44 -46.13 55.20 5.39E+01 7.09E-02 2.0052216 17036.36 8.518
Total 100.0000 5.25E+00 100.0000 5.39E+01 7.10E-02 2.006
'The Properties of Gases and Liquids,Reid,Prausnitz,Sherwood,Third Edition / ?
"See ref.Document VOC Emissions from Batch Chemical Processes.
% vLlJ
VR2,cfh=Air Flow,cfh x P,mmHg/[P-(Sum X`VP)],mmHg
2013 Estimated Emissions for Alan III Condenser Seal Pots
Seal Pots Ethylene Glycol Diethylene Glycol 1,4-Dioxane VOC Data Entry for GR 3 and GR6
h Ibl r Ib/hr Ibi r Ib/hr Ib! r Ibthr Ibt r
VT-205A 0.0460 383.16 ----- 0,0460 38316
VT-206A 1.13E-03 1.92E-01 6.76E-07 1.15E-04 5.50E-05 9.34E-03 1.18E-03 0.20
VT-305A/306A 1.54E-03 1.31 E+01 5.26E-07 4.47E-03 5.89E-05 5.01 E-01 1.60E-03 13.61
VT-405A/406A 1.01E-03 0.00E+00 4.35E-07 0.00E+00 6.02E-05 0.00E+00 1.07E-03 0.00
VT-605/606 1.21 E-03 1.03E+01 3.23E-07 2.74E-03 6.07E-05 5.16E-01 1.27E-03 10.83
Total 5.09E-02 4.07E+02 1.96E-06 7.33E-03 2.35E-04 1.03E+00 5.12E-02 407.80
Total VOC(ton/yr) 0.204
j
T 3 C
_ 1'7� r Z d !IQ/N T 3 o co /3
Cyr c 5 /6�H T 2 c G 1j rl T ��5- //T 4/0 V 13
w r'
APT 7-0/ 301/3
hi i 1c / h 4P-7 yoi d
kIr 6 d s /fiT6o& '4 -
AR-7301 -
pe -/ 40l
N7 3a3'A/f/ 7 504. 4
}-/ 7' yoS.►lWrY06A
1 6/24/2014 f, A T� Cl A . AEI Calculations 2013
/-/-r ,sa 5 /S/14-7s t✓6 /3 ,

FO8-Alan IV Condenser Seal Pots
Basis
Emissions are estimated based on vapor-liquid equilibrium under air sweep conditions.
Air sweeping rate was assumed to be 600 scfh. �+
As a conservative assumption,100%of saturation in air after sweeping was assumed.
Seal Pot Operating Data C
Actual Flow Rate Max.Temp. Room
Seal Pots Reactors Temperature
m Ib/hr C C
VT-205B/206B APT-201B 160 80,064 40 25
VT-3058/3068 APT-301B 130 65,052 40 25 VT-405B/406B APT-4018 135 67,554 40 25 V 5 (� L// L H `/
VT-505 APT-501 35 17,514 40 25
Seal Pot Configurations
Seal Pots Tank Size Liquid Height Max Capacity Working
Volume
L(ft) W(tt) H(ft) ft gal gal
VT-205B/206B 5.0 0.8 3.0 2.75 89.8 82.3
VT-305B/306B 5.0 0.8 3.0 2.75 89.8 82.3
VT-405B/406B 5.0 0.8 3.0 2.75 89.8 82.3
VT-505 5.0 1.0 3.0 2.75 112.2 102.9
Test Data of Liquid Compositions
Seal Pots Ethylene Glycol Dleth Iene Glycol 1,4-Dioxane
pm wt% ppm wt% ppm wt%
VT-205B/206B 69,900 6.99 1,700 0.17 18.8 0.0019
VT-305B/306B 94,000 9.40 1,300 0.13 19.8 0.0020
VT-405B/4068 63,000 6.30 1,100 0.11 20.7 0.0021
VT-505 75,000 7.50 810 0.08 20.7 0,0021
Compositions determined through sampling and analysis in November 1994
6/24/2014 AEI Calculations 2013

1
Emis. calculations
VT-20513/2066
Tank Capacity 89.8 gal
Working Volume 82.3 gal
Air Sweep Rate 600.0 cfh
Operation Time 8,496.0 hr/yr
Gas Constant 999 mmHg-cf/Ibmol-K
IT,
y, In f z MOW Ci l -" Qo d;3 n5"jpdC@,CF :-_:r 11i t9IS't, ,sV " ,Cfh.
40 760 600.00 100 1.0 0.0024 645.90
Cdrri" i5ent... Wf%.:. r:" :Iti/lb0lof Abittpll3b tl,. X>tt3Dl°� A. B ,' VRgamrxski , VP mm >_ ,.Y":." .. Po R'.Ib7hr„. lb/ .°
Ethylene Glycol 6.9900 62.069 1.13E-01 2.1379 20.2501 6022.18 -28.25 0.41 8.80E-03 1.16E-05 0.0011276 9.58 0.005
Dieth lene Glycol 0.1700 106.122 1.60E-03 0.0304 17.0326 4122.52 -122.50 0.01 3.08E-06 4.06E-09 0.0000007 0.01 0.000
1,4-Dioxane 0.0019 88.107 2.13E-05 0.0004 16.1327 2966.88 -62.15 74.62 3.02E-04 3.98E-07 0.0000550 0.47 0.000
Water 92.8381 18.015 5.15E+00 97.8313 18.3036 3816.44 -46.13 55.20 5.40E+01 7.11 E-02 2.0084710 17063.97 8.532
Total 1 100.0000 5.27E+00 100.0000 5.40E+01 7.11 E-02 2.010
VT-305B/306B
Tank Capacity 89.8 gal
Working Volume 82.3 gal
Air Sweep Rate 600.0 cfh
Operation Time 8,496.0 hr/yr
Gas Constant 999 mmHg-cf/lbmol-K
� piriiriH' fowYCfh etoa �aee C ,. , , ,fs
f�
40 760 600.00 100 1.0 0.0024 645.51
Co ent _' �_ Wt;:°lo-,. . ;:ib?lbmsai':Ibnabi bmaii, ,�, ��1o1°la.,.,. « �,� Ate ; ,F. B,s �,�„A-: Cr�� ,M.4,.�V ° """f;� .� ,"mmH' ° Y,.,"�,>,.. :.ER;'iblltr�„-°`.ib �- ;-•tC .r=-
Ethylene Glycol 9.4000 62.069 1.51E-01 2.9267 20.2501 6022.18 -28.25 0.41 1.20E-02 1.58E-05 0.0015427 13.11 0.007
Dieth lene Glycol 0.1300 106.122 1.23E-03 0.0237 17.0326 4122.52 -122.50 0.01 2.40E-06 3.16E-09 0.0000005 0.00 0.000
1,4-Dioxane 0.0020 88.107 2.25E-05 0.0004 16.1327 2966.88 -62.15 74.62 3.24E-04 4.26E-07 0.0000589 0.50 0.000
Water 90.4680 18.015 5.02E+00 97.0492 18.3036 3816.44 -46.13 55.20 5.36E+01 7.05E-02 1.9912056 16917.28 8.459
Total 100.0000 5.17E+00 100.0000 5.36E+01 7.05E-02 1.993
6/24/2014 AEI Calculations 2013

VT-4uot5/406B
Tank Capacity 89.8 gal
Working Volume 82.3 gal
Air Sweep Rate 600.0 cfh
Operation Time 0.0 hr/yr
Gas Constant 999 mmHg-cf/Ibmol-K
�- ��
40 760 600.00 100 1.0 0.0024 646.02
Ethylene Glycol 6.3000 62.069 1.01E-01 1.9160 20,2501 6022.18 -28.25 0.41 7.89E-03 1.04E-05 0.0010107 0.00 0.000
Dieth lene Glycol 0.1100 106.122 1.04E-03 0.0196 17.0326 4122.52 -122.50 0.01 1.98E-06 2.61 E-09 0.0000004 0.00 0.000
1,4-Dioxane 0.0021 88.107 2.35E-OS 0.0004 16.1327 2966.88 -62.15 74.62 3.31E-04 4.35E-07 0.0000602 0.00 0.000
Water 93.5879 18.015 5.20E+00 98.0640 18.3036 3816.44 -46.13 55.20 5.41 E+01 7.12E-02 2.0136129 0.00 0.000
Total 1 100.0000 1 5.30E+00 1 100.0000 1 5.41 E+01 7.12E-02 2.015
VT-505
Tank Capacity 112.2 gal
Working Volume 102.9 gal
Air Sweep Rate 600.0 cfh
Operation Time 8,496.0 hr/yr
Gas Constant 999 mmHg-cf/lbmol-K
s '
a /ice i
a„ E Al/40 760 600.00 100 1.2 0.0030 645.83
ER blftc„ ip F
Ethylene Glycol 7.5000 62.069 1.21E-01 2.3009 20.2501 6022.18 -28.25 0.41 9.47E-03 1.25E-05 0.0012134 10.31 0.005
Dieth lene Glycol 0,0810 106.122 7.63E-04 0.0145 17.0326 4122.52 -122.50 0.01 1.47E-06 1.94E-09 0.0000003 0.00 0.000
1,4-Dioxane 0.0021 88.107 2.35E-05 0.0004 121327 2966.88 -62.15 74,62 3.34E-04 4.39E-07 0.0000607 0.52 0.000
Water 92.4169 18.015 5.13E+00 97.6841 18.3036 3816.44 -46.13 55.20 5.39E+01 7.09E-02 2.0052216 17036+36 8.518
Total 1 100.0000 1 5.25E+00 1 100.0000 1 5.39E+01 7.10E-02 2.006
'The Properties of Gases and Liquids,Reid,Prausnitz,Sherwood,Third Edition
"See ref.Document VOC Emissions from Batch Chemical Processes.
VR2,cfh=Air Flow,cfh x P,mmHg/[P-(Sum X'VP)],mmHg 1 / 'T C✓-1 U i/,�,Q 13 )Z
2013 Estimated Emissions for Alan IV Condenser Seal Pots �/ 1
x
n ' Data Entry for GR 3 and GR6
VT-205B/206B 1.13E-03 9.58E+00 6.76E-07 5.74E-03 5.50E-05 4.67E-01 1.18E-03 10.05
VT-305B/306B 1.54E-03 1.31E+01 5.26E-07 4.47E-03 5.89E-05 5.01E-01 1.60E-03 13.61
VT-405B/406B 1.01E-03 0.00E+00 4.35E-07 0.00E+00 6.02E-05 0.00E+00 1.07E-03 0.00
VT-505 1.21E-03 1.03E+01 3.23E-07 2.74E-03 6.07E-05 5.16E-01 127E-03 10.83
Total I 4.89E-03 I 3.30E+01 I 1.96E-06 1.30E-02 2.35E-04 1.48E+00 5.13E-03 34.49
Total VOC(ton/ r) 0.017
6/24/2014 AEI Calculations 2013

F09 -Valves, Pump Seals, Flanges, and Open-Ended Lines
Basis
- Alan III/IV esterification vessel liquid ethylene glycol(EG)concentration are based on the maximum concentration in those reactors.
- Alan III/IV esterification vessel vapor EG concentration is based on vapor-liquid equilibrium calculations using the maximum liquid concentration in the reactors.
- The lowest pressure, highest temperature scenario is used as a worst case scenario to calculate vapor composition for the Alan III/IV esterification vessels.
Operating Data
Liquid
Operating EG
Hours Wt%
Alan III Esterification (EG transfer) 8,496 100.00
Alan IV Esterification (EG transfer) 0 100.00
Glycol Recovery Distillation 8,760 91.58
Glycol Recycle Distillation 8,760 60.59
Esterification Vapor Concentration Calculations
Maximum Liquid EG
Concentration 3 %wt(in vessels)
Temperature 274 F
134.4 C
Pressure 16 psig
1,587.4 mm Hg (abs)
Components Wt% MW Liquid Mole Antoine Coefficients VP PP Y Vapor Weight
Ib/Ibmol _Ibmol to A B C mmHg mmHg Ibmol lb /a
EG 3 62.069 0.0483 0.0089 20.2501 6022.18 -28.25 79.43 0.71 0.0004 0.0276 0.1062
Water 97 18.015 5.3844 0.9911 18.3036 3816.44 -46.13 2310.75 2290.19 1.4427 25.9902 99.8938
Totals 100 5.4327 1.0000 1 1 1.4431 26.0179 100.0000
Ir0cj
0 3 3 .L
6/24/2014 AEI Calculations 2013

Fugitive Emissions
Equipment Number of Emission Factor VOC Emissions
Units
k /hr/source Ib/hr/source lb/hr. IbI r
Esterification Vessels(Alan III &Alan IV)
Valves(heavy liquid) 8 0.00023 5.07E-04 0.0041 17.23
Connectors(gas/vapor) 6 0.00183 4.03E-03 2.57E-05 0.11
Connectors(heavy liquid) 16 0.00183 4.03E-03 0.0646 274.21
Subtotal 0.0686 291.55
Glycol Recovery Distillation System (CL-2)
Valves (heavy liquid) 10 0.00023 5.07E-04 0.0046 40.68
Pump Seals 4 0.00862 1.90E-02 0.0696 609.82
Open-ended Lines 4 0.0017 3.75E-03 0.0137 120.27
Connectors(heavy liquid) 20 0.00183 4.03E-03 0.0739 647.31
Subtotal 0.0880 770.76
Glycol Recycle Distillation System (CL-1)
Valves(heavy liquid) 10 0.00023 5.07E-04 0.0031 26.91
Pump Seals 4 0.00862 1.90E-02 0.0461 403.46
Open-ended Lines 4 0.0017 3.75E-03 0.0091 79.57
Connectors(heavy liquid) 20 0.00183 4.03E-03 0.0489 428.27
Subtotal 0.0582 509.94
Total VOC 0.2148 1,5 2-.2
Total VOC (ton/yr) 0.79 f✓ �� 2-
6/24/2014 AEI Calculations 2013

F10 - Terephthalic Acid Storage Silos (VT-2, VT-3, VT-33)
Basis
- Particulate emissions from the TPA silos and transfer system are estimated based on nitrogen consumption.
- It is assumed that the nitrogen used in the TPA silos and transfer system is 85% of the total facility wide nitrogen consumption.
- It is assumed that 0.11 grains of TPA is emitted per cubic foot of nitrogen through equipment leaks.
2012 Facility wide Nitrogen Consumption 45,818 Mcf/yr
Percentage of Facility wide Consumption in TPA 85 %
2012 TPA Nitrogen Consumption 38,945.3 Mcf/yr
Amount of TPA in Nitrogen 0.11 grains/cf N2
1.57E-05 Ib/cf N2
2013 TPA(PM) Emissions 612.00 Ib TPA/yr
0.306 ton TPA/yr
PM = PM10 = PM2.5
Olt Q S ZC-)
6/24/2014 AEI Calculations 2013

} F11 - Fiber Beaming &Take-Up
Basis
- Finish oils are used in fiber beaming and take-up operation.
- Emissions are estimated based on the annual finish consumption for each finish component used containing VOC and their respective VOC concentration.
- As a worst case scenario, it is assumed that all VOC contained in the finishes is emitted.
Emission Calculations
Annual Annual VOC Emissions
Product Consumption VOC CASRN HAP/TAP wt%
lb! r I I Ib/ r ton! r
Silquest A-187 4,463 Methanol 67-56-1 H 0.1 4.46 0.002
Cirrasol G3780A 478 Ethylene Glycol 107-21-1 H 3 14.34 0.007
Gero on WS-251 0 Iso ro anol 67-63-0 19 0.00 0.000
CoatOSil7602 147 VOC NA 13.3 19.55 0.010
Monawet MO-70R 475 Propylene Glycol 57-55-6 20 95.00 0.048
Fluffton 1556 N211 6,325 VOC NA 1 70 4427.50 2.214
Dow Corning 2-8818 Polyoxyethylene 61827-42-7 3 83.37 0.042
Emulsion 2,779 Isodec I Alcohol
Ethylene Glycol 107-21-1 H 3 83.37 0.042
Acetic Acid 64-19-7 T 1.1 28.77 0.014
Bioban DXN Antimicrobial 2,615 Acetaldehyde 75-07-0 H,T 0.1 2.62 0.001
Vinyl Acetate 108-05-4 H 0.1 2.62 0.001
Crotonaldeh de 4170-30-3 0.1 2.62 0.001
TRYFAC 5576 0 VOC NA 0.8 0.00 0.000
Raneoff FX-880 0 VOC NA 0.47 0.00 0.000
ITOTALVOCI 4,764.20 1 2.382 .�- d S C/
HAP/TAP Summary
HAP/TAP Annual HAP Emissions
I
tout r
Acetaldehyde 2.62 0.001
Acetic Acid 28.77 0.014 1
Ethylene Glycol 97.71 0.049 /' e
Methanol 4.46 0.002 V J
Vinyl Acetate 2.62 0.001 r
TOTAL HAP 136.17 0.068
6/24/2014 AEI Calculations 2013

F12-Maintenance Solvents
Basis
It is assumed that 100%all HAP/TAP and non-VOC,ozone-depleting chemicals contained in each solvent is emitted,as a worst-case scenario.
Where an MSDS specifies VOC content for a mixture,this number prevails over any individual concentrations of organic compounds and is used to determine air emissions for that mixture.
Where VOC content is not provided for the mixture,100%of smaller chained VOCs(e.g.,isobutane,heptane,etc.)and 10%of the larger,more complex VOCs(e.g.,mineral oil,petroleum
distillates,etc.)that are contained in the mixture are assumed to be emitted,as a worst-case scenario.
As a general rule,where the MSDS lists a concentration range,the midpoint is used,and where a'less than"is provided,the nearest whole number below that value is used.
Annual PFI Solvent Consumption
2012
Product Organic Container Amount/ 2012 Product Annual
Wt% SG %Volatile
Description Components CASRN HAPITAP Size,Type Container Consumption VOC
Emissions
MSDS I AEI MSDS AEI MSDS lb/container #Conti r Ib/ r Ib/ r
Trichloroeth lene 79-01-6 H T 90-99 94.5 386.55
Lectra Clean CRC 1 2-Bu lene Oxide 106-88-7 H 0.50 0.5 1.46 @70F 1.46 100 20 oz.can 1.90 215 409.05 2.05
Hydrotreated Petroleum 64742-52-5 10.00 1.0 0.23
FEL-PRO He tane 142-82-5 20.00 20.0 1.14 1.14 Not Provided 16 oz.can 1.19 19 22.58 4.52
Antiseize Hexane 110-54-3 H T 20.00 20.0 4.52
Isobutane 75-28-5 20.00 20.0 4.52
LUBT,Anti-seize Mineral Oil 64742-52-5 1 55-60 Not
w/nickel Oxygenated Proprietary 10-15 7.0 1.1 1.1 Provided 16 oz.can 1.15 109 125.00 8.75
Aliphatic
Solvent Naphtha
LPS Presolve (Petroleum) 64742-88-7 30-50 10.0 0.808 0.808 100 11 oz.can 0.58 1 0.58 0.06
cleaner/degreaser Medium Aliphatic
d-Limonene 5989-27-5 50-70
Polyglycol 25852-47-5 5-10 2.6 0.00
Dimethacrylate
Acrylic Acid 79-10-7 H 5-7 6.0 0.00
Loctite Master Cumene 80-15-9 1-3 2.0 1.1 @ 80F 1.1 VOC 13.0% 6 oz.can 0.43 0 0.00 0.00
Gasket Hydro eroxide
Ethylene Glycol 107-21-1 H 1-3 2.0 0.00
1-Acetyl-2- 114-83-0 0.1-1 0.45 0.00
Phen Ih drazine
Severely
Brute Lube Cutting H drotreated Not Not Not
Fluid Paraffinic Distillate Provided Provided 10 0.923 0.923 Provided 16 fl.oz. 0.96 43 41.38 4.14
Chlorinated Paraffin
Chlorinated Fatty
Odorless Mineral 8052-41-3 <5 0.4 0.00
Sprayon Belt Spirits Not 1.00 75 12 oz can 0.78 0 0.00
Dressing Methyl Chloroform 71-55-6 HIT 45 45 Provided 0.00
Isobutane 75-28-5 10 10 0.00
Aliphatic Petroleum 8052-41-3 50
Distillates
WD 40 A-70 Hydrocarbon 32.50 0.710 @ 0.710 80 11 oz.spray 0.51 111 56.48 18.36
Pro ellant 68476-85-7 25 70F can
Petroleum Base Oil 64742-65-0 >15
Trichlorotrifluoroeth T,Not a
76-13-1 75 75 10.74
CRC Contact ane VOC 1.57 1.57 100 20 oz. 2.05 7 14.32
Cleaner Chlorodifluorometha 75-45-6 Not a VOC 25 25 Aerosol can 3.58
ne
IT r i 2,
6/24/2014 CIS IV Z AEI Calculations 2013
1 Z-_

2012
Product Organic Wt% SG %Volatile Container Amount/ 2012 Product Annual
Description Components CASRN HAP/rAP Size,Type Container Consumption VOC
Emissions
MSDS I AEI MSDS AEI MSDS lb/container #Cont.! r lb,' r lb/ r
2-Buto ethanol 111-76-2 5-7
Speedball Ethanolamine 141-43-5 1-3 9.25 1.00 1.00 98.00 32 fl.oz. 2.09 83 173.06 16.01
Nonyl Phenol 9016-45-9 1-1.5 Plas.bottle
Ethoxylate
Elf Keystone 1,1-Dichloro-l- Not 17.64 oz.
spinneret spray fluoroethane 1717-00-6 Not a VOC Provided 50 1.24 1.24 90 wt.12 1.10 0 0.00 0.00
110 Dimeth I of siloxan 63148-62-9 Not 40 cans/case 0.00
Chlorodifluorometha 75-45-6 Not a VOC 40 40 0.00
Spinneret spray, ne 1.19-1.21 1.2 87 14 oz.wt 12 0.88 0 0.00
SPRAYON#524 1,1-Dichloro-l- 1717-00-6 Not a VOC 50 50 cans/case 0.00
fluoroethane
Tetrasodium Salt of 64-02-8 1-5
EDTA
J-Shop 600 Alkylphenoxy 26027-38-3 1-5 5 gal.
Cleaner Polyethoxyethanol 8.33 1.00 1.00 VOC 8.33+/ Bag/box 41.70 0 0.00 0.00
Sodium Xylene 1300-72-7 1-5 combo.
Sulfonate
2-Buto ethanol 111-76-2 5-10
pinneret spray, 1,1,1,2- 811-97-2 Not a VOC 40 40 87%(50% 12 oz.wt 12 92.40
SPRAYON PART Tetrafluoroethane 1.23 1.23 VOC) cans/case 0.75 308 231.00
#500522, 1-Bromo ro ane 106-94-5 50 50 115.50
Goo Gone Proprietary VOC 99.90 99.90 0.764 0.764 VOC 99.9 55- al. 350.45 0 0.00 0.00
Goo Gone Proprietary VOC 99.90 99.90 0.764 0.764 VOC 99.9 8 fl.oz. 0.40 3 1.19 1.19
TOTAL 673.10
Emission Summary(Contactor&PFI)
Classification Component Annuall missions
[777ZT7nlr
Acrylic Acid 0.00 0.00 +00 it
1,2-Butylene Oxide 2.05 1.02E-03 ~ _ ;
HAP Ethylene Glycol 0.00 0.00E+00
Hexane 4.52 2.26E-03
Trichloroeth lene 386.55 1.93E-01
Total 393.11 0.20
Non-HAP VOC All 173.26 0.09
Total VOC HAP&Non HAP 566.38 0.28
is oro- -
fluoroethane 0.00 0.00E+00
Non-VOC Ozone- Chlorodifluoromethane 3.58 1.79E-03
Depleting Methyl Chloroform 0.00 0.00E+00
1,1,1,2-Tetrafluoroethane 92.40 4.62E-02
Trichlorotrifluoroethane 10.74 5.37E-03
Total 106.72 0.05
6/24/2014 AEI Calculations 2013

F15-Spray Condenser Recycle Feed Tank(VT-532)
Basis
Emissions are estimated based on vapor-liquid equilibrium under air sweep conditions.
Air sweeping rate was assumed to be 600 scfh.
As a conservative assumption, 100%of saturation in air after sweeping was assumed.
Tank Operating Data
Actual Flow Rate Max.Temp. Room
Tank Reactors Temperature
m Ibfhr C C
VT-532 APT-101,104. 3 1.501 2 40 25
107A/B
Tank Configuration
Tank Size Liquid Height Recirculation Max Capacity Working
Tank Rate Volume
L(ft) W(ft) H(ft) ft gpm gal a)
VT-532 4.0 1.5 3.3 2 75 11 148 1 123 4
Test Data of Liquid Compositions
Tank Ethylene Glycol Diethylene Glycol Acetaldehyde 1,4-Dioxane
ppm wt% ppm Wt% ppm wt% ppm wt%
VT-532 37,500 3.75 405 0.0405 11 0.0011 52 0.0052
'Condensers(C-112/113 A/B)are secondary spray condensers used to remove any remaining vapors that carry over from the
primary C110/111 A/B condensers.Therefore C-112/113 remove less EG and DEG than other vessel seal pots,such as seal pot VT-
605/606.VT-532 is assumed to have 50%less EG and DEG than the amount of EG and DEG found in seal pot VT-605/606.
"Sampling(9/28/98)and analysis by EPA Method 305 determined the concentration of acetaldehyde and 1,4-dioxane in VT-532.
v
� S 3c(
6/24/2014 / AEI Calculations 2013
�2

Emission Calculations
VT-532
Tank Capacity 148.1 gal
Working Volume 123.4 gal
Air Sweep Rate 600.0 cfh
Gas Constant 999 mmHg-cf/Ibmol-K
Volof Free
Temp,°C P,mmH Air Flow,cfh %Sat Space,cf n,lb mols VR2,cfh
40 760 600.00 100 3.3 0.0080 646.43
Com onent Wt.% I MW,Ib/ibmol Ibmol/Ibmatl X,mol% A B C VP,mmHg X*VP,rnrnHgj Y ER,Ib/hr IN r ton/ r
Ethylene Glycol 3.7500 62.069 6.04E-02 1.1186 20.2501 6022.18 -28.25 0.41 4.60E-03 6.06E-06 0.0005905 5.17 0.003
Dieth lene Glycol 0.0405 106.122 3.82E-04 0.0071 17.0326 4122.52 -122.50 0.01 7.17E-07 9.43E-10 0.0000002 0.00 0.000
Acetaldehyde 0.0011 44.054 2.50E-05 0.0005 16.2481 2465.15 -37.15 1504.77 6.96E-03 9.15E-06 0.0006333 5.55 0.003
1,4-Dioxane 0.00520 88.107 5.90E-05 0.0011 16.1327 2966.88 -62.15 74.62 8.15E-04 1.07E-06 0.0001485 1.30 0.001
Water 96.20 18.015 5.34E+00 98.8728 18.3036 3816.44 -46.13 55.20 5.46E+01 7.18E-02 2.0315166 17796.09 8.898
Total 100.00 5.40E+00 100.00 5.46E+01 7.18E-02 2.033
*The Properties of Gases and Liquids,Reid,Prausnitz,Sherwood,Third Edition
**See ref.Document VOC Emissions from Batch Chemical Processes.
VR2,gal/hr=Air Flow(cfh)x P,mmHg/[P-(Sum X*VP)],mmHg
2013 Estimated Emissions for Spray Condenser Recycle Feed Tank(VT-532)
Tank Ethylene Glycol Diethylene Glycol Acetaldehyde 1,4-Dioxane VOC
Ib/hr Ibl r Ib/hr Ibl r Ib/hr Ibi r Ib/hr Ib/ r Ib/hr Ib! r
VT-605/606 5.90E-04 5.17E+00 1.57E-07 1.38E-03 6.33E-04 5.55E+00 1.48E-04 1.30E+00 1.37E-03 1.20E+01
Total VOC(ton/ r) 6.01E-03
6/24/2014 2 AEI Calculations 2013

F16 - Polymer Sump
Basis
- Condensed liquid from process condensers along with vacuum pump cooling water and distillation column
overheads flow by gravity to an in ground, concrete sump. A large sump pump transfers the water from the
sump to two process cooling towers (TW-2 and TW-3)where it is cooled and pumped back to the building
for re-use in process heat exchangers. The sump is covered with non-air tight metal sheeting.
- Fugitive emissions from the sump are estimated based on sump dimensions, sampling results and the
emission model TOXCHEM+.
- Assumptions are the detection limit for each of the compounds and no emissions control attributable to
the covering plates over the sump.
Source Acetaldehyde 1,4-Dioxane VOCs
Ib/hr Ib/ r Ib/hr Ib/ r Ib/hr Ib/ r ton/ r
Polymer Sump 0.112 984 8.79E-03 77 0.121 1,061 0.531
T F
S 3 5�
6/24/2014 AEI Calculations 2013

Emergency Generator
IEG-2
Manufactured Date: 1994 l� i
Reconstructed Date: NA
Engine Type: Spark Ignition (SI) < x `� '✓
Fuel Type: Propane
Operation Type: Emergency Only v
Rated Power: 38 BHp
Operation Time: 26 hrs/yr
Annual Energy Usage: 988 hp-hr/yr
2.514 MM BTU/yr
Propane Heating Value: 91.5 MM BTU/103 gal
Annual Fuel Usage: 0.027 103 gal/yr
Emission Estimate Method: AP-42, Section 1.5 (Liquefied Petroleum Gas Combustion)
Emission Actual Emissions
Pollutant Factor
Ib/103 qal Ib/ r tonl r
Criteria Air Pollutants
Total PM 0.60 0.02 8.24E-06
Filterable PM-10 0.60 0.02 8.24E-06
Filterable PM-2.5 0.60 0.02 8.24E-06
NOx 19.00 0.52 2.61 E-04
CO 3.20 0.09 4.40E-05
SO2" 0.21 0.01 2.95E-06
VOC 0.50 0.01 6.87E-06
Total HAP N/A ----- -----
Largest HAP N/A ----- -----
Greenhouse Gas (GHG) Emissions
CO2 12,500 343.42 0.17
CH4 0.20 0.01 0.00
N2O 0.90 0.02 0.00
Toxic/Hazardous Air Pollutants
None ----- -----
*SO2 emission factor= 0.1 S, where S is the amount of sulfur in propane (grains/100ft)

Propane Sulfur Content
Sulfur content in propane calculated according to the maximum ethyl mercaptan content(50 ppm)
as provided in suppliers MSDS.
S + C2H6 --> C21-16S
50 lb C,HrS x 1 mole C,H.S x 1 mole S x 32 lb S
106 lb Propane 62 lb C21-16S 1 mole CAS 1 mole S
25.8 lb S
106 lb Propane
25.8 lb S x 7.000 grains S x 11.9 lb Propane
106 lb Propane lb S 100 ft3 Propane
2.1497 grains S
100 ft3 Propane
Since Total HAP<0.5 tpy(1,000 Iblyr)and each Criteria pollutant<5 tpy,this emission unit is
an 'Insignificant Activity" by definition in accordance with 15A NCAC 02Q .0503(8).

Emergency Generator
IEG-3
Manufactured Date: 2005
Reconstructed Date: NA
Engine Type: Spark Ignition (SI)
Fuel Type: Propane
Operation Type: Emergency Only .
Rated Power: 78 BHp
Operation Time: 26 hrs/yr
Annual Energy Usage: 2,028 hp-hr/yr VI)
5.160 MM BTU/yr
Propane Heating Value: 91.5 MM BTU/103 gal "low
Annual Fuel Usage: 0.056 103 gal/yr
Emission Estimate Method: AP-42, Section 1.5 (Liquefied Petroleum Gas Combustion)
Emission Actual Emissions
Pollutant Factor
Ib/103 gal Ib/ r ton/yr
Criteria Air Pollutants
Total PM 0.60 0.03 1.69E-05
Filterable PM-10 0.60 0.03 1.69E-05
Filterable PM-2.5 0.60 0.03 1.69E-05
NOx 19.00 1.07 5.36E-04
CO 3.20 0.18 9.02E-05
SO2* 0.21 0.01 6.06E-06
VOC 0.50 0.03 1.41 E-05
Total HAP N/A ----- -----
Largest HAP N/A
Greenhouse Gas (GHG) Emissions
CO2 12,500 704.92 0.35
CH4 0.20 0.01 0.00
N2O 0.90 0.05 0.00
Toxic/Hazardous Air Pollutants
None ----- I -----
*SO2 emission factor= 0.1 S, where S is the amount of sulfur in propane (grains/100ft)

Propane Sulfur Content
Sulfur content in propane calculated according to the maximum ethyl mercaptan content(50 ppm)
as provided in suppliers MSDS.
S + C21-16 —> CAS
50 lb C,HrS x 1 mole C,HrS x 1 mole S x 32 lb S
106 lb Propane 62 lb C21-16S 1 mole CAS 1 mole S
= 25.8 lb S
106 lb Propane
25.8 lb S x 7,000 grains S x 11.9 lb Propane
106 lb Propane lb S 100 W Propane
= 2.1497 grains S
100 W Propane
Since Total HAP< 0.5 tpy(1,000 Ib/yr)and each Criteria pollutant<5 tpy,this emission unit is
an 'Insignificant Activity"by definition in accordance with 15A NCAC 02Q .0503(8).

Inorganic Chemical Storage Tanks
The table below summarizes the inorganic chemical storage at the facility.
Tank ID Contents I Ca aci al
IVT-235 Caustic 12,000
IVT-236 Caustic 12,000
IVT-237 Caustic 12,000
IVT-238 Caustic 12,000
IVT-239 Caustic 12,000
INT-1 Nitrogen 13,000 cf
Since none of the inorganic chemicals stored contribute to emissions of HAP or
criteria pollutants, each tank is an "Insignificant Activity" by definition in accordance
with 15A NCAC 02Q .0503(8).
Sources not Required to Report for AEI:
Storage tanks: ii) used solely to store inorganic liquids.
C

Propane Storage Tank
IHT-9
Liquefied Petroleum Gas (LPG) is stored at the facility in a 30,000 gallon tank and is used as a
backup fuel for the Steam Superheaters (HE-553 & HE-554)and the Pyrolysis Ovens (OV-1 &
OV-2). The table below shows the typical composition of LPG.
LPG Com osition
Com onent Concentration VOC
Propane 87.5 - 100% Yes
Ethane 0-7% No
Propylene 0-5% Yes
Butanes 0-2.5% Yes
Ethyl Mercaptan 0 -50 ppm Yes
Assuming that 1,2-Epoxybutane is not present, LPG
contains no HAP.
Since LPG is stored under pressure,there is negligible VOC emissions under normal
storage conditions. Therefore this tank is an "Insignificant Activity" by definition in
accordance with 15A NCAC 02Q .0503(8).
1 �/T

Fuel Oil Storage Tanks
Fuel oil is used throughout the facility as a fuel for both emergency-related and process-
related stationary combustion units. No. 6 Fuel Oil is used as a backup supply for Boilers SG-
1 and SG-2 and for Dowtherm Heaters HE-3, HE-4 and HE-5. No. 2 Fuel Oil (diesel) is used
in Emergency Generator EG-1 and for both Emergency Fire Pumps (CP-28 and CP-593).
The table below summarizes the fuel oil storage at the facility.
IHT-8 Diesel 7270
,000 G
IVT-14 No. 6 Fuel Oil0,000 (� -1 3
IHT-18 Diesel900
IHT-22 Diesel © 3 7
. IHT-23 Diesel 270
IVT-30 No. 6 Fuel Oil 30,000
IVT-44 No. 6 Fuel Oil 60,000
IVT-45 No. 6 Fuel Oil 235,000
The only criteria pollutant that may be emitted as a result of the transfer and storage of fuel
oils is VOC. Based on a MSDS review of the fuel oils used at the facility(No. 2 and No. 6),
neither contain any HAP and the vapor pressures of both fuels are very low(see below).
Vapor Pressures
No. 2 Fuel Oil (Diesel): 0.009 psia @ 70°F
No. 6 Fuel Oil: <0.1 psia @ 70°F
Due to the extremely low vapor pressures of both oils, none of the tanks could ever
emit VOC of 5 tpy or more, regardless of their annual throughputs. Therefore each tank
is an 'Insignificant Activity" by definition in accordance with 15A NCAC 02Q .0503(8).
No. 6 FUEL OIL TANKS EMISSIONS
Fuel
Throughput: 624 gallons
Emissions
(lbslyr(Total)) 0 G'�
VOC VOC i Z
Tank ID %of Total Emissions Emissions
y r) (ton/ r)
IVT-45 68% � 0 0.00E+00 C
IVT-44 16% 0 0.00E+00
IVT-30 8% 0 0.00E+00
IVT-14 8% 0 0.00E+00
Totals 0 0 1

DIESEL FUEL TANKS EMISSIONS
Fuel
Throughput: 1879 gallons
Emissions
(Ibs/yr(Total)) 0.98
VOC VOC
Tank ID % of Total Emissions Emissions Q
.r -I
IHT-22 8`io 0.0784 3.92E-05
IHT-23 8% 0.0784 3.92E-05 S `� 7
IHT-8 57% 0.5537 2.77E-04
IHT-18 27% 0.2646 1.32E-04
Totals 0.9751 0.0005

Gasoline Storage Tanks
Tank Data J
Chemical Stored Gasoline Gasoline
Max.Concentration% 100 100
Dimensions Gasoline Composition-CITGO Gasolines(All Grades)
Type Horizontal Horizontal from MSDS
Shell Length(ft) 4.08 10.50
Shell Diameter(ft) 4.OB 4.00
Maximum Liquid Height(ft) - - 25 15.63 H Toluene I _
Average Liquid Height(it) - - 20 12.50 Pentanes L
Working Volume(gal) 971 987 20 12.50 Octanes = I
Max.Turnovers per Year 2 0 18 11.25 H Xylenes O
Max.Throughput(galtyr) 1,943 0 23 14.38 H Hexanes 05
Is Tank Heated No No 15 9.38 Heptanes
Is Tank Underground No Noo 10 6.25 Ethanol
5 313 H Benzene
Shell Characteristics 8 100 Trimethylbenzenes
Shall Color/Shade Alum/Diff Alum/DiH
Shell Condition Good Good 4 2.50 H Cumene
4 2.50 H Ethylbenzene
Roof Characteristics 3 1.88 Cyclohexano
Color/Shade - - 2 1.25 Cyclopentane
Condition - - 2 1.25 H Naphthalene
Type - - 1 0.63 H Styrene
Height(ft) - - 160 10l'
Radius(ft) - -
Total HAP Estimated Composition 51,25%
Breather Vent Settings
Vacuum Setting(psig) 0 0
Pressure Settin 0 0
Output from TANKS Software(Version 4 0 9dl-see Section 2 for detailed output
Unleaded Gasoline Storage Tank(IHT-15)
HAPNOC 22.07 1032.94 1,055.01 0.52751 Toluene 10.97
Total HAPNOC 0.52751 Xylene 2.17
Hexane 58.18
224-Trimeth(benzene 3.95
Benzene 7.73
Cumene 0.58
Eth(benzene 0.58
Naphthalene 0.01
S rene 0.10
From Tanks Detailed Report
Unleaded Gasoline Storage Tank(IHT-21)
III
VOC V 0 0.00
AP/VOC 0 0.00 0.00 0.00000 Toluene 0.00
Total HAPNOC 0.00000 Xylene 0.00
Hexane 0.00
2 2,4-Trimeth Ibenzene 0.00
Benzene oto
Cumene 0.00
Eth Ibenzene 0.00
Na hthalene 0.00
S rene 0.00
•'From Tanks Detailed Report
The estimated Total HAP composition in the
Unleaded Gasoline used at the facility is 52.73%.
Therefore,HAP emissions from each tank Is
assumed to be<1,000 lb/yr.Since Total HAP<
O.S tpy(1,000 Iblyr)and VOC<5 tpy for each
storage tank,each is an"Insignificant Activity"
by definition in accordance with 15A NCAC 020
.0503(8).

Alan IV Copolymer Extruder
IXT-506
A portion of the polymer produced in the Alan IV train is directed to a twin screw extruder
where other materials are added to produce a polyethylene terephthalate (PET) copolymer.
Vapors generated during extrusion are removed by a vacuum pump and condensed in a
cooler. Any oil released from the oil-sealed vacuum pump is removed by an oil mist
eliminator before the air is vented to the atmosphere.
Before controls, the extruder has the potential-to-emit(PTE) 0.25 Ib/hr(1.095 tpy) non-HAP
VOC and 0.39 Ib/hr(1.708 tpy) PM (see permit application in HSE Department Air Files for
more detailed information -ATM 6.21).
Alan IV Copolymer Extruder did not operate in 201�.

IVT-1
Esterification Mix&Feed Tanks
A series of tanks and mixers are used to prepare the Ethylene Glycol(EG)and Terephthalic Acid(TPA)mixture for the polymerization
process that produces Polyethylene Terephthalate(PET),or Polyester,at the facility. Additionally,a small amount of Diisopropylamine
(DIPA)is added to the mixture for pH control and an even smaller amount of a metal-based compound is added to catalyze the reaction.
The identification of each tank/mixer is provided in the table below,along with a description of its vent,as applicable:
TarrkltD1T .•.r., =PitiCess .. . uentD®§cri"lfon ...i, .:';
VT-02A/B TPA Feed Tanks Vents back to closed-loop nitrogen syste
VT-06AB EG Batch Make-Up Tanks Both tanks vent into process area
VT-08A/B EG Feed Tanks Vents back to VT-06A/B
VT-13A/B DIPA Measuring Tanks Vents back to storage tank(VT-78)
MX-14A/B Paste Mixers Vents back to closed-loop nitrogen syste
As depicted in the table above,the only atmospheric vent associated with the Esterification Mix&Feed Tanks is from the EG Batch Make-
Up Tanks(VT-06A/B),where EG and DIPA are added.
Calculation Basis
Emissions are assumed to occur both when charging each batch make-up tank(vapor displacement)and continuously through evaporation.
Vapor displacement emissions are calculated using the Ideal Gas Law and evaporative emissions are calculatied utilizing a diffusion
equation presented in the EPA Off-site Consequence Analysis Guidance Document,5/24/96. Component vapor pressures are estimated
using Antoine's Equation and coefficients obtained from'The Properties of Gases and Liquids",Reid,Prausnitz,Sherwood,Third Edition,
and component partial pressures are estimated using Raoulfs Law.
Vapor displacement emissions are based on the amount of EG and DIPA charged into each tank per batch and the maximum production
capacity of the train in which each batch make-up tank serves. It is assumed that the charging temperature is equal to the operation
temperature(65 C)of the batch make-up tanks,as a worst-case scenario.
Evaporative emissions are based on the operationtemperature(65 C)and the total exposed liquid surface area within the batch make-up
tanks(as derived on p.1-30). There is no air or nitrogen purge in either tank and the liquid surface is not subject to any air movement or
ventilation within the process area. Therefore,evaporative emissions are essentially negligible. However,it is assumed that there is a 0.01
m/s air flow over the liquid surface,as a worst-case scenario. It is also assumed that the liquid surface is continually exposed 8,760 hr/hr.
Physical Properties 8,Equations
�Camo erit�*EIN
CASR84Fteg#, An#oh�eCoefficients f
Ethylene l co . 2 , 62.069
Diiso ro lamine(DIPA) 108-18-9 5.98 101.193 15.6973 2807.94 -51.20
Antoine's Equation: Partial Pressure Equation(Raoufl's Law):
In Pi=A-B/(C+T) PP=PixXi
where: Pi = Vapor pressure of VOC @ T,mm Hg where: PP=Partial pressure of VOC in mixture,mm Hg
A,B,C=Antoine Coefficients Pi = Vapor pressure of VOC @ T,mm Hg
T = Temperature,"K Xi = Mole fraction of VOC in mixture
Ideal Gas Equation(Charging): Evaporative Loss(Diffusion)Equation:
m=(PI xAxVxMW�/(RxT) QR=(0.0035xU°-'xMWmxAx PP)/T
where: m = VOC emitted,Ib/hr where: QR = Evaporation rate of VOC,lb/min
Pi = Vapor pressure of VOC @ T,mm Hg U = Air displacement rate,m/s
Xi = Mole fraction of VOC in mixture MW = Molecular weight of VOC,Ib/lbmol
V = Rate of displacement,cfh A= Surface area of mix tank,sf
MWi = Molecular weight of VOC,Ibfibmol PP=Partial pressure of VOC in mixture,mm Hg
R = Gas constant,999 mm Hg cfAbmol°K T = Temperature,"K
T = Temperature,"K
li

Surface Area(A)Evaluation
The exposed surface area of the liquid within the EG Batch Make-Up Tanks that is subject to evaporation is assumed to be the curved
surface area(CSA)of a cone(due to a vortex formed while mixing)with a diameter equal to the inside diameter of the tank and a depth
equal to its radius(as a worst-case scenario). Both tanks have an inside diameter of 89 5/8 inches.
Circumference of tank=21tr C
CSA
s d= A<
(unwrapped cone) B
C Length of arc AB=2nr
s=Slant Height Area of sector ABC Arc length AB of sector ABC
r Radius d Depth
Area of circle with centerl(iii Qmference of circle with center at C
=
Pythagorean Theorem Area of sector ABC = 2nr
ns2 2ns
s2=r2+d2
=2r2 d=r Area of sector ABC = nrs
s =r (2)12 Therefore:
Area of sector ABC = nrs = Curved Surface Area(CSA) = nr2(2)112
Radius of VT-06A/B(89 5/8'inside diameter) 3.73 ft each
Surface Area(A)of Liquid during mixing 61.96 ft`each
Alan III(VT-06A)Emissions
Avg.Alan III PET Capacity 11,004 Ib/hr
96.395 1,000 Ib/vr
EG Required 99,200 1,000lb/vr
3,000 lb/batch
323.12 gal batch
DIPA Required 432.00 1,000IbM
13.06 lb/batch
2.19 gaVbatch
Batches/yr 33,067
Charging(per batch)
EG U.M9 3.000 48.33 0.997
DIPA 101.193 13.06 0.13 0.003 15.6973 2807.94 -51.20 369.38 0.984
Charging Losses
Max.Charging Temperature 338.15 K(65 C)
Total Charging
Emissions
Com onent Iblbatch ib! r
EG 0.01793 592 76
DIPA 0.00009 2.85
Evaporative Losses
Area Air Displacement Rate 0.01 m/s
Mix Tank exposed surface area 62.0 ft2
Max.Evaporative Temperature 338.15 K(65 C)
Total Evaporative
V.Press. P.Press. Emissions
Com onent MW Mote Frac. mm Hq mm Ha Ib/hr Ibf r
EG 62.069 0.997 2.26 2.259 0.63752 328.71
DIPA 101.193 0.003 369.38 0.984 0.02265 198.38
Total Emissions(Charging+Evaporative)
colri nont`_ ,
EG 921.47
DIPA 201.23
Total VOC 1,122.7
122.70 p_

Alan IV(VT-06B)Emissions
Avg.Alan IV PET Capacity 0 lb/hr
0 1,000 Iblyr
EG Required 0 1,000 Ib/yr
2,000 lb/batch
215.4 gallbatch
DIPA Required 0.00 1,000 lb/yr
0.00 lb/batch
0.00 gallbatch
Batches/yr 0
Charging(per batch)
ffic 77
Q Corn tt mw'1111,^'4t wo likii M atI
EG 62.069 2,000 1 3222 1 1000 6022..18 -28.2F 2.26 2.265
.00 20.2501
DIPA 101.193 0' 0 5
Z
0.00 0.0'0 15.6973 2807. ?0 369.38 0.000
Charging Losses
Max.Charging Temperature 338.15 K(65 C)
mi,onen
I E1,21ib;-UPP"
EG 0'01198 1 0.00
DIPA 0.00000 0.00
Evaporative Losses
Area Air Displacement Rate 0.01 m/s
Mix Tank exposed surface area 62.0 It'
Max.Evaporative Temperature 338.15 K(65 C)
.....2... ',�-,-Total Evaporative
VV blyr
' rn ffdAtW;Ab&r9tN 4 L_
EG 62.069 0.997 2.26 2.259 0.03752 328.71
DIPA 101.193 0.003 369.38 0.984 0.02265 198.38
Total Emissions(Charging+Evaporative)
EG 0.00
DIPA 0.00
Total VOC 0.00

Tire Application Lab
ITL
The Tire Application Lab is a non-process operation that consists of a Litzler Unit and two tire
presses to assist our manufacturing process to better serve customers that our fiber to
manufacture tires. The Litzler Unit consists of a small covered dip container, where fiber
samples are coated with a dip finish followed by an electric oven. The processes and presses
are vented to the atmosphere for industrial hygiene purposes. There are no known quantifiable
emissions from the tire presses. The worst-case dip finish material in the Litzler Unit contains
37% formaldehyde by weight, which is a North Carolina Toxic Air Pollutant(TAP), as well as
federal Hazardous Air Pollutant(HAP) and Volatile Organic Compound (VOC). The fiber dip
usage will be small (89.5 grams per batch).
In Performance Fibers Submission of Insignificant Activities, it was calculated that 0.0125
pounds/hour of formaldehyde was emitted when hours of operation is 2080 hours/year.
The table below the actual emissions from 2010, based on hours of operation.
Formaldehyde Formaldehyde VOC
(VOC) Hours of
Emission Operation Emissions Emissions
Factor(lb/hr) (Ib/yr) (ton/yr)
0.0125 832 10 0.01
C, Cr d

Parts Washers (Maintenance Areas)
IMPW
Four(4) parts washers are used in maintenance areas throughout the facility for the
purpose of cleaning and degreasing metal parts. The chemical used in each washer is
100% petroleum distillate (CASERN 64742-47-8) and contains no HAP. The petroleum
distillate has a density of 6.7 lb/gal, a flash point of 148 F and a vapor pressure of only 0.2
mmHg@68F.
Every 12 weeks (4 times/yr), a vendor drains each parts washer, removes the sludge,
replenishes each with virgin petroleum distillate, and takes the spent distillate/sludge offsite
for recovery and/or proper disposal.
The table below shows the capacity of each parts washer and the total amount of
petroleum distillate used in each on an annual basis.
30 4 804
30 4 804
70 4 1,876
80 4 2,144
VOC Emissions (ton/yr) 2.8

Triethylene Glycol (TEG) Cleaning Unit(ITEGCU)
The TEG cleaning unit(autoclave)is used primarily for the cleaning of spinnerettes,which are used in the spindraw
process at the facility. TEG is a stable,odorless,slightly viscous(S.G. 1.1255 @ 20 C)non-HAP VOC liquid of
extremely low vapor pressure(<0.01 mm Hg @ 20 C).
TEG is added to the system from 55-gallon drums. The autoclave lid is hydraulically operated,enabling it to be
tightly sealed during the system's 16 hr/day operating cycle. Prior to and following each cycle,the system is purged
with nitrogen to remove any combustion supporting oxygen. Once the cleaning cycle begins,the temperature and
pressure in the system is operated at 265 C and 18 psig. The autoclave is protected by a pressure relief valve set at
25 psig and a rupture disc designed to open at 35 psig. The nitrogen purges described above and any emergency-
related vents from the autoclave are directed through a knock-out pot located above the cleaning room on the roof,
where TEG can be collected and drained back into the system as necessary. Following the cleaning cycle,the
autoclave is not opened until the temperature and pressure are reduced to 65 C and 0 psig. Periodically,spent TEG
is removed from the system and sent offsite for recovery and purification,which helps to prevent emergency vents
during operation due to water build-up in the system.
The table below summarizes the venting scenarios associated with the operation of this system:
Scenario IDuration/Temperatul Emissions
TEG Addition 10 min @ ambient Negligible
Pre-Operation Nitrogen Purge 5 min @ ambient Negligible
System Operation 16 hours @ 2650C Emergency vent only
Post-Operation Nitrogen Purge 5 min @ 650C Negligible
Opening Autoclave 10 min @ 650C Negligible
System Draining 110 min @ ambient lNegligible
The next table shows the vapor pressures of TEG at different operating temperatures:
log(P)=A-B/(t+C) Equation and coefficients obtained from literature published by
where P,mm Hg;t,C The Dow Chemical Company
A 7.6302007 t,C P,mm H
B 2156.4581 20 0.0001
C 165.92442 65 0.0196
265 422.6103
Due to the extremely low vapor pressure of TEG under normal operating conditions,the TEG system could never
emit VOC in excess of 5 tpy(-1,065 gal/yr). The system typically uses no more than two 55-gallon drums per month
(-12,390 Ib/yr),most of which is sent offsite for recovery and purification.
Since Total potential VOC emissions is<5 tpy,the Triethylene Glycol(TEG)Cleaning Unit is an
"Insignificant Activity"by definition in accordance with 15A NCAC 02Q.0503(8).
TEG USED TEG SENT OFF-SITE TEG BALANCE PRODUCT EMISSIONS, EMISSIONS,
(GALLONS) (GALLONS) (GALLONS) DENSITY(LB/GAL) LB/YR TON/YR
1.760 1.760 0 9.42 0 0
05 C 410
0

TANf'"!,4.0 Report of 6
TANKS 4.0.9d
Emissions Report - Detail Format
Tanki Indentification and Physical Characteristics
j
Identification
User Identification: ES16
City: New Hill
State: North Carolina
Company: Performance Fibers,Inc.
Type of Tank: Vertical Fixed Roof Tank
Description: Spent Ethylene Glycol Tank(VT-20) _
Tank Dimensions
Shell Height(ft): 30.25
Diameter(ft): 34.00
Liquid Height(ft): 30.25
Avg.Liquid Height(ft): 15.13
Volume(gallons): 205,450.07
Turnovers: 0.17
Net Throughput(gai/yr): 34,675.00
Is Tank Heated(y/n): N
Paint Characteristics
Shell Color/Shade: White/White
Shell Condition Good
Roof Color/Shade: White/White
Roof Condition: Good
Roof Characteristics
Type: Dome
Height(ft) 4.65
Radius(ft)(Dome Roof) 17.00
Breather Vent Settings
Vacuum Settings(psig): 0.00
Pressure Settings(psig) 0.00
Meterological Data used in Emissions Calculations:Raleigh,North Carolina(Avg Atmospheric Pressure=14.53 psia)
Till://C\Program Files\Tanks409d\summarydisplayhtm ! j 6/2/2014

TArfi'p 4.0 Report F 2 of 6
TANKS 4.0.9d
Emissions Report - Detail Format
c P -Liquid Contents of Storage Tank,
ES16--Vertical Fixed Roof Tank
New Hill,.North Carolina .
Liquid.
Daily Liquid.Surf. Bulk Vapor Liquid Vapor
Temperature(deg F) Temp Vapor Pressure(psia) Mal. Mass Mass Mal. Basis for VaponPressure
Mixture/Component Month Avg. Min.' Max. (deg F) Avg. Min. Max. Weight. Fract. Fract. Weight Calculations
Spent Ethylene Glycol All 61.17 55.60, 66.73. 59.30 - 0.1645 0.1355 0.2014 18.1349 34.82 .
Ethylene Glycol 0.0012. 0.0009 0.0016 62.0690 0.6800 0.0093 62.67 Option 1:VP60=.001095 VP70 q..001774
Water q 0.2653 0.2185 03247 18.0150 0.3200 0.9907 18.02 Option.1:VP60=.252846 VP70=.359616
r °file:%/C:\Program Files\Tanks409d\sumrnarydisplay.htm ' . ? :6/2/2014

TAIL"l-4.0 Report F 3 of 6
TANKS'4.0.9d
Emissions Report -'Detail format
E Detail Calculations (AP-42)
ES16'-.Vertical Fixed Roof Tank
New Hill;,North Carolina
Annual Emission Calceulations'
Standing Losses(lb): 127.2200
Vapor Space Volume(cu ft): 15,895.8539
Vapor Density(lb/cu ft): 0.0005
Vapor Space Expansion Factor. 0.0473
Vented Vapor Saturation Factor.- 0.8675
Tank Vapor Space Volume:
Vapor Space Volume(cu ft): .15,895.8539
Tank Diameter(ft):. 34.0000
Vapor Space Outage(ft): 17'5080
Tank Shell Height(ft): 30.2500
Average Liquid Height(ft): 15.1250
Roof Outage(ft):. 2.3830
Roof Outage(Dome Roof)
Roof Outage(ft): 2:3830
Dome Radius(ft): 17.0000
Shell Radius(ft): 17.0000
Vapor Density
Vapor Density(Ib/cu ft): 0.0005
Vapor Molecular Weight(lbAb-mole): 18.1349
Vapor Pressure at Daily Average Liquid
Surface Temperature(psia): 0.1645
Daily Avg.Liquid Surface Temp.(deg.R): 520.8354.
Daily Average Ambient,Temp.(deg.F): 59.2833
Ideal Gas Constant R'
(psis cult/(lb-mol-deg R)): .16.731 '
Liquid Bulk Temperature(deg.R): 518.9733
Tank Paint Solar Absorptance(Shell): 0.1700
Tank Paint Solar Absorptance(Roof): 0.1700.
Daily Total Solar Insulation,
Factor(Btu/sgft day): 1,393.0797
Vapor Space Expansion Factor
Vapor Space Expansion Factor.. 0.0473
Daily Vapor Temperature Range(deg.R): 22.2671
Daily Vapor Pressure Range(psia): 0.0659
Breather Vent Press.Setting Range(psia): 0.'0000
Vapor Pressure at Daily Average Liquid
Surface Temperature(psia): 0.1645
Vapor Pressure at Daily Minimum Liquid
Surface Temperature,(psia): 0.1355
Vapor Pressure at Daily Maximum Liquid
Surface Temperature(psia): 0.2014
Daily Avg.Liquid Surface Temp.(deg R): 520.8354,
Daily Min.Liquid Surface Temp.(deg R): 515.2687
Daily Max.Liquid Surface Temp.(deg R): 526.4022
Daily Ambient Temp.Range(deg.R): 21.7167
.Vented Vapor Saturation Factor
Vented Vapor Saturation Factor: 0.8675
Vapor Pressure at Daily Average Liquid:
Surface Temperature(psia):. 0.1645
Vapor Space Outage(it): '17.5080
le-M\Program Files\Tanks409d\summarydisplay.htrn - . " . ' ' i' , 6/2/2014

TAbw!r:4:O We port'
Working Losses(lb): 2.4634
Vapor Molecular Weight(lb/lb-mole): 18.1349
Vapor Pressure at Daily.Average Liquid:
Surface Temperature(psia): 0.1645'
Annual Net Throughput(gal/yr.): 34,675,0000
Annual Turnovers:.. 0:1688 s
Turnover Factor:. 1.0000
Maximum Liquid Volume(gal): 205,450.0687
3 Maximum Liquid Height_(ft): 30.2500.
Tank Diameter(ft)i 34.0000 y
Working Loss Product Factor: 1:0000
Total Losses(lb): 129.6835 -
i
file://(:\Program Files\Tanks409d\summarydisplay.htm _. 6/2/2014? s I�

AYT-7-c�:CO Report :� . :�, . , � �, � . :z; F;_r :<<5 ,0f 6
TAN K8 4.0.9d .. .
Emissions Report - Detail Format
Individual Tank Emission Totals t ..
Emissions°Report for: Annual
ES16-Vertical Fixed Roof Tank,:
New Hill, North Carolina.
Losses(lbs)
Components Working.Loss Breathing Loss Total Emissions
Spent Ethylene Glycol 2.461 129.68
Water- . JF, 2:44 ------------
126.03 128:48
Ethylene Glycol 0.02 1.19 1.21
filt:WC:\Pr+ogram Eiles\Tanks409d\sumiriarydispla htm s t6% /20 '4 �. '>

TAINT_-,,4.0 Report i. - I F;- 1 of 6
TANKS 4.0.9d
Emissions Report- Detail Format
r. i Tank Indentification and Physical Characteristics°
Identification
User Identification: ES17
City: New Hill
State: North Carolina
Company: Performance Fibers,Inc.
Type of Tank: Vertical Fixed Roof Tank
Description: Virgin Ethylene Glycol Tank(VT-19)
Tank Dimensions
Shell Height(ft): 30.25
Diameter(ft): 34.00
Liquid Height(ft): 30.25
Avg.Liquid Height(ft): 15.13
Volume(gallons): 205,450.07
Turnovers: 9.59
:Net Throughput(gal/yr): 1,970,746.09
Is Tank Heated(y/n): N 3
Paint Characteristics
Shell Color/Shade: Gray/Medium
Shell Condition Good
Roof Color/Shade: Gray/Medium
Roof Condition: Good
Roof Characteristics
Type: Dome
Height(ft) 4.65
Radius(ft)(Dome Roof) 17.00
Breather Vent Settings
Vacuum Settings(psig): -0.03
Pressure Settings(psig) 0.03
Meterological Data used in Emissions Calculations:Raleigh,North Carolina(Avg Atmospheric Pressure=14.53 psia)
file:!/C.Wrogram Files\Tanks409d\summarydisplay.htm 6/2/2014

rr :TAT7-P 4 O Rep6rt _ �.t 6
TANKS 4.0.9d „
Emissions Report Detail Format
. : Liquid Contents of Storage Tank .
E$17-Vertical Fixed Roof Tank
New Hill,.North Carolina `
Liquid
Daily Liquid Surf. Bulk Vapor Liquid Vapor
Temperature(deg F) Temp Vapor Pressure(psia) Mol. Mass Mass Mol. Basis for Vapor Pressure
Mixture/Component Month Avg. Mina Max. (deg F) Avg:. ., Min. Max. Weight. Frail. Tract. Weight Calculations
'Ethylene Glycol All 68.49 57.95. 79.03 62.36' 0.0017 0.0010 0.0027 62.0690 62.07 Option 1;VP60=.001095 VP70=.001774
' 1
$j2/2fl14i
ffi1e-Y/C:\Program Files\Tanks409d\summarydi§play htm f ' !

:I .'i'AT " �4.0 Report - - -1 t - _ - '-)' �'-f I _ ; , - : - - :IF-�.'�3 d£6 . .
t
TANKS 4.0.9d
Emissions Report - Detail Format
Detail Calculations (AP-42)'
E917-.Vertical fixed Roof-Tank
New Hill, North Carolina
Annual Emission Calcaulations
Standing Losses(lb): 8.0397
Vapor Space Volume(cu ft): 15,895:8539
Vapor Density(lb/cu ft): 0.0000
Vapor Space Expansion Factor. 0.0758
Vented Vapor Saturation Factor. 0.9985
Tank Vapor Space Volume:
Vapor Space Volume(cu ft): ,15,895.8539
Tank Diameter(ft): 34.0000
Vapor Space Outage(ft): 17.5080
Tank Shell Height(ft): 30.2500
Average Liquid Height(ft): 15.1250
Roof Outage(ft):. 2.3830
Roof Outage(Dome Roof)
Roof Outage(ft): 2.3830
Dome Radius(ft):. 17.0000
Shell Radius(ft): 17.0000
Vapor Density
Vapor Density(Ib/cu fl): 0.0000
Vapor Molecular-Weight(lb/Ib-mole): 62.0690
Vapor Pressure at Daily Average Liquid
Surface Temperature(psia): 0.0017
Daily Avg.Liquid Surface Temp.(deg.R): 528.1618
Daily Average Ambient Temp.(deg.F): 59.2833
Ideal Gas Constant R
(psia cult/(lb-cool-deg R))i .10.731
Liquid Bulk Temperature(deg.R): 522.0333
Tank Paint Solai Absorptance(Shell): 0.6800'
Tank Paint Solar Absorptance(Roof): 0.6800
Daily Total Solar Insulation
Factor(Btu/sgft day): 1,393.0797
Vapor Space Expansion Factor
Vapor Space Expansion Factor: . 0.0758
Daily Vapor Temperature Range(deg.R): 42.1602
Daily Vapor Pressure Range(psia): 0.0017
Breather Vent Press.Setting Range(psia): 0.0600
Vapor.Pressure at Daily Average Liquid
Surface Temperature(psia): 0.0017.
Vapor Pressure at Daily Minimum Liquid
Surface Temperature(psia): 0.0010
Vapor Pressure at Daily Maximum Liquid
Surface.Temperature(psia): 0.0027.
Daily Avg.Liquid Surface Temp.(deg R): 528.1618
Daily Min.Liquid Surface Temp.(deg R): 617.6217
Daily Max.Liquid Surface Temp.(deg R): 538.7018
Daily Ambient Temp.Range(deg.R): 21.7167
Vented Vapor Saturation Factor
Vented Vapor Saturation Factor. 0.9985
Vapor Pressure at Daily Average Liquid:
Surface Temperature(psis): 0.00.17
Vapor Space Outage(it): 17.5080
file%/C:1Program Files\Tafiks409d\summarydisoldy.htin. . . s' 1 6%2/�201'4

TAIL' "':,0 Report
��� � �� � � 'a `s3 �� s .• a; � d, .t ,.,�, c3 ' �' F va 4;of°,6 r,
Working Losses(Iti): .4.8684
Vapor Molecular Weight(Ib/Ib-mole): 62.0690
Vapor Pressure at`Daily Average Liquid:
Surface Temperature(psia): 0.0o17
Annual Net Throughput(gaWr.): 1,970,746.0897
Annual Turnovers: 9.5923.
Turnover Factor: 1.0000 .
Maximum Liquid Volume(gal): 205,450.0687 '
Maximum Liquid.Height(ft): 30.2500.
Tank Djameter(ft): 34.0000
Working Loss Product factor:. 1.0000
Total Losses(lb): 12.9081
z" k fileJ/C.-Wrogram Files\Tanks409d\sW=arydisplay.litm ; _ I f . . 6/2/2a14

TAN, ' 1A`Report. S . 1 ,1.._ I F, 5-0£�6
��
TANKS 4.0.9d
Emissions Report - Detail Format
i. ' +. =Individual Tank Emission Totals '
�Y 11
Emissions Report for: Annual
ES17-Vertical Fixed Roof Tank
New Hill, North Carolina
Losses(lbs)
Components f Working.Loss Breathing Loss Total Emissions
Ethylene Glybol 4.87 8.04 1 12.91
file%/C:\Program Files\Tanks409d\suinmarydi§pla'y.litm :;' ; ' i ,r ; 6/2/2014i `I F

A ;'
5 A �1 R ----,.Uofi6
TA77-P�4.0 Report 1
TANKS 4.0.9d
Emissions Report - Detail Format
i Tank Indentification and Physical Characteristics
Identification
User Identification: ES18
City: New Hill
State: North Carolina
Company: Performance Fibers, Inc.
Type of Tank: Vertical Fixed Roof Tank
Description: Virgin Ethylene Glycol Tank(VT-34)
Tank Dimensions
Shell Height(ft): 30.25
Diameter(ft): 34.00
Liquid Height(ft): 30.25
Avg.Liquid Height(ft): 15.13
Volume(gallons): 205,450.07
Turnovers: 9.59
Net Throughput(galtyr): 1,970,745.06
Is Tank Heated(y/n): N
Paint Characteristics
Shell Color/Shade: Gray/Medium
Shell Condition Good
Roof Color/Shade: Gray/Medium
Roof Condition: Good
Roof Characteristics
Type: Dome
Height(ft) 4.65
Radius(ft)(Dome Roof) 17.00
Breather Vent Settings
Vacuum Settings(psig): -0.03
Pressure Settings(psig) 0.03
Meterological Data used in Emissions Calculations:Raleigh,North Carolina(Avg Atmospheric Pressure=14.63 psia)
6/2/2014 i1e:/YC:\Program Files\Tanks409d\suinmatydispldy.htin,

_ .,TAW-',-4-4 0 Report . r �.' a _ a. F 2 of 6
1. TANKS 4.0.9d
R Emissions Report- Detail format
Liquid Contents of Storage Tank
ES18 -!Vertical Fixed Roof Tank
New Hill; North Carolina
Liquid
Daily Liquid Surf.' Bulk Vapor Liquid Vapor -
Temperature(deg F)- Temp Vapor Pressure(psia) Mol. Mass Mass Mol. Basis for Vapor Pressure
Mbdure/Component Month Avg. Mina Max. (deg F) Avg. Min. Max. Weight. . Fract. Frect. Weight Calculations
Ethylene Glycol All 66.49 57.95 79.03 62.36 0.0017 0.0010 0.0027• 62.0690 62.07 Option 1:V060=,001095 VP70=.001774 .
file-//C:\Program Files\Tanks409d\sumtmarydisplay.htrn - ' . 6/,2/2014

TAN ",.4.0 Report F; 3 of 6
T ANKS 4.0.9d
Emissions Report - Detail Format
ins (
Detail Callcuaafo AP-42)
E818 Vertical Fixed Roof Tank = :
New Hill, North Carolina
Annual Emission Calcaulations
Standing Losses(lb): 8.0397
Vapor Space Volume(cu ft): 15,895.8539
Vapor Density(lb/cu ft): 0.0000
Vapor Space Expansion Factor. 0.0758
Vented Vapor Saturation Factor: 6.9985 "
Tank Vapor.Space Volume:
Vapor Space Volume,(cu ft): "15,896.8539' -
Tank"Diameter(ft): 34.0000
Vapor Space Outage(ft): 17:5080
Tank Shell Height(ft): .30.2500
Average Liquid Height(ft): 15.1250
Roof Outage(ft):. 2.3830
Roof Outage(Dome Roof)
Roof Outage](ft): 2:3830.
Dome Radius(ft): 17.0000
Shell Radius(ft): 17.0000
Vapor Density
Vapor Density(lb/cu ft): 0.0000
Vapor Molecular Weight(IbAb-mole): 62:0690
Vapor Pressure at Daily Average Liquid
Surface Temperature(psia): 0.0017
Daily Avg:Liquid_Surface Temp.(deg.R): 528.1618'
Daily Average Ambient Temp.(deg.F): '59.2833
Ideal Gas Constant R
(psis cult/(lb-mol-deg R)): .10.731 '
Liquid Bulk Temperature(deg.R)i '522.0333
Tank Paint Solar Absorptance(Shell): 0.6800
Tank Paint Solar Absorptance(Roof): 0.6800
Daily Total Solar Insulation.
Factor(Btu/sgft day): 1,393.0797
Vapor Space Expansion Factor
Vapor Space Expansion Factor: 0.0758.
Daily Vapor Temperature Range(deg.R): 42.1602
Daily Vapor Pressure Range(psia): 0.0017
Breather Vent Press.Setting Range(psia): 0.0600
Vapor Pressure at Daily Average Liquid
Surface Temperature(psia): 0.0017
Vapor Pressure at Daily Minimum Liquid
Surface Temperature(psia): 0.0010
Vapor Pressure at Daily Maximum Liquid,
Surface Temperature(psia):' 0.0027 ,.
Daily Avg.Liquid Surface Temp.(deg R): 528.1618
Daily Min.Liquid Surface Temp.(deg R): 517.6217
Daily Max.Liquid Surface Temp:(deg R): 538.7018. "
Daily.Ambient Temp.Range(deg..R): 21.7167
Vented Vapor Saturation Factor "
Vented Vapor Saturation Factor: 0.9985.
Vapor Pressure at Daily Average Liquid:,
Surface Temperature(psia): .' 0.0017
Vapor Space.Outage.($): 17.5080
f le://C:\Program.Files\Tank"s409d\summarydisplay.htin 6%2/2014, 7: 4

:T�";4:0 Report ! ' - ).. y ? F 4 of 6
Working Losses(lb): 4.8684
Vapor Molecular Weight(IbAb-mole): 62.0690
Vapor Pressure at Daily Average Liquid
Surface Temperature.(psia): 0.0617
Annual Net Throughput(gal/yr.): 1,976,745.0625
Annual Turnovers: 9.5923
Turnover Factor: 1.0000
Maximum Liquid Volume(gal): 205,450.0687
Maximum Liquid Height(ft): 30.2500
Tank Diameter(ft)::. 34.0000
Working Loss Product Factor: 1.0000
Total Losses(lb): 12.9081
s +file; /CAPrograrii'Files\Tanks409d\summarydisp1#1tm 16/2/2014!a

TAN, .1.0 Report 5 "of 6 .
TANKS 4.0.9d
Emissions Report - Detail-Format
a, Individual Tank Emission Totals:
z _
r,
Emissions Report for: Annual
ES18 ' Vertical Fixed.Roof Tank:
New Hill, North Carolina
Losses(lbs)
Components Working Loss Breathing Loss Total Emissions
Ethylene Glycol 4.87 8.04 1 12.91
;i 6/2/2014
sfile:%/QAPr'Ogram Files\Tanks409d\summary�display.htm'

TAN7 ,4:0 Report - v ; ; F; 1 .of 6
Q TANKS 4.0.9d
Emissions Report - Detail Format
:Tank Indentification and-Physical Characteristics
Identification
User Identification: ES19
City: New Hill
State: North Carolina
Company: Performance Fibers, Inc.
Type of Tank: Vertical Fixed Roof Tank
Description: DIPA Holding Tank(VT-78)
Tank Dimensions
Shell Height(ft): 14.00
Diameter(ft): 12.00
Liquid Height(ft): 14.00
Avg.Liquid Height(ft): 7.00
Volume(gallons): 11,844.41
Turnovers: 1.96
Net Throughput(gal/yr): 23,220.00
Is Tank Heated(y/n): N
Paint Characteristics
Shell Color/Shade: Aluminum/Diffuse
Shell Condition Good
Roof Color/Shade: Aluminum/Diffuse
Roof Condition: Good
Roof Characteristics
Type: Dome
Height(ft) 1.33
Radius(ft)(Dome Roof) 9.00
Breather Vent Settings
Vacuum Settings(psig): -0.03
Pressure Settings(psig) 0.03
Meterological Data used in Emissions Calculations:Raleigh,North Carolina(Avg Atmospheric Pressure=14.53 psia)
: . file://C \Program Files\Tanks409d\sumhiarydigpliy.htm T 6/2/2014

! . T Y _0.4.0 Report i of 6
TANKS 4.0.9d
Emissions Report Detail format
y. ;• ; . Liquid Contents of Storage Tank'
E$19-Vertical Fixed Roof Tank "
New Hill, North Carolina',..
Liquid
Daily Liquid Surf. Bulk Vapor Liquid Vapor
Temperature(deg F) Temp Vapor Pressure'(psia) Mol. Mass Mass Mol. Basis for Vapor Pressure
Mixture/Component Month Avg. Min.' Max. (deg F) Avg.' Min. Max. Weight. Fract. Frad. Weight Calculations
Diisopropylamine All. 67.34 57.58 77.10 61.88 1.1436, 0.8759 1.4757 .101.1930 101.19 Option 1:VP60=.931393 VP70=1.220367
file://C:\]Rrog'ram?Files\Tariks409d\summarydis'play.htm ' i rf F ' 3 6/2/2014 1 a' �'

TATS 4.0'Report F ` 3 of 6
TANKS 4.0.9d
Emissions Report Detail Format
r: ;. Detail Calculations (AP-42)
ES19-Vertical'Fixed Roof Tank i
New Hill North Carolina
Annual Emission Calcaulations.
Standing Losses(lb): 506.2467
Vapor Space Volume(cu ft): 868.1229
Vapor Density(lb/cu ft): 0.0208 _
Vapor Space Expansion Factor., 0.1144
Vented Vapor Saturation Factor. 0.6825
Tank Vapor Space Volume:
Vapor,Space Volume(cu ft): 868.1229
Tank Diameter(ft): 12.0000
Vapor Space Outage(ft): 7.6759
Tank Shell Height(ft): 14.0000
Average Liquid Height(ft); 7.0000
Roof Outage(ft): 0.6759
Roof Outage,(Dome Roof)
Roof Outage(ft):, 0.6759
Dome Radius(ft):, 9.0000
Shell Radius(ft): 6.0000
Vapor Density
Vapor Density(lb/cu ft): 0.0205
Vapor Molecular Weight(Ib4b=mole): 101.1930
Vapor Pressure at Daily Average Liquid
Surface Temperature(psia): 1.1436
Daily Avg:Liquid Surface Temp.(deg.R): 527.0125 ,
Daily Average Ambient Temp.(deg.F): 59.2833
Ideal Gas Constant R
(psia cuft/(lb-mol-deg R)): 16.731
Liquid Bulk Temperature(deg.R).' 521.5533
Tank Paint Solair Absorptance(Shell);. 0.6000
Tank Paint Solar Absorptance(Roof): 0.6000
Daily Total Solar Insulation .
Factor(Btu/sgft day): 1,393.0797
Vapor Space Expansion Factor
Vapor Space Expansion Factor: 0.1144
Daily Vapor Temperature Range(deg.R): 39.0397
Daily Vapor Pressure Range(psia): 0.5998
Breather Vent Press.Setting,Range(psia): 0.0600
Vapor,Pressure at Daily Average Liquid
Surface Temperature(psia): 1.1436
Vapor Pressure atrDaily Minimum Liquid
Surface Temperature,(psia): 0.8759
Vapor Pressure at Daily Maximum Liquid.
Surface Temperature(psia): 1.4757
Daily Avg.Liquid Surface Temp.(deg R): 527.0125
Daily Min.Liquid Surface Temp.(deg R): 517.2526
'Daily Max.Liquid Surface Temp,(deg R): 536.7725
Daily Ambient Temp.Range(deg.R): 21.7167
Vented Vapor Saturation Factor' .
Vented Vapor Saturation Factor.' 0.6825 .
Vapor Pressure at Daily Average Liquid:
Surface Temperature(psia): 1t1436
Vapor Space Outage(ft); ' . 7.6759
file://C:\Program,Files\Tanks409d\s'ummarydispldy.htfn 612/2014 y'' 1

TAT"': 4.0 Report]. ; 3 ; t'. : . , . t F 410 6
Working Losses(16): 63.9775
Vapor Molecular Weight(lb/lb-mole): 101.1930
Vapor Pressure at Daily Average Liquid
Surface Temperature(psia): 1.1438
Annual Net Throughput(gaVyf•): 23,220.0000 s
Annual Turnovers: ft 1:9504 . .
Turnover Factoc, '- -1.0000 n• . .
Maximum Liquid Volume(gal): 11,844.4147
MaximumLiquid.Height(ft): 14.0000.
Tank.Diameter(ft): 12.0000
Working Loss Product'Factoc 1.9600
Total Losses(Ib): 570.2242
:I
;: ; fileJ/CAProgram.Files\Tanks409d\summarydisplay.htm' S' ! a ; 6/2/201'4

�TArn � U'Report € i F S of,6:r
s
•
TANKS 4.0.9d
.Emissions Report Detail format
Individual Tank Emission Totals
'. Emissions Report for: Annual
ES19-Vertical Fixed Roof Tank
New Hill, North Carolina.
Losses(lbs).
Components Working Loss Breathing Loss I Total Emissions
Diisopropylarnine 63.96 50625 1 570.22
`file:Y/OVrogram Files\Tafiks409d\su' arydisplayhtm. r 6/2/2014
�.

,TAIW�P4.0 Report C.
F=-"-
.I afi6;
i TANKS 4.0.9d
Emissions Report - Detail Format
Tank Iridentification and Physical Characteristics
Identification
User Identification: ES30
City: New Hill
State: North Carolina
Company: Performance Fibers, Inc.
Type of Tank: Horizontal Tank
Description: Distillation Column Bottoms Purified EG Tank(HT-25)
Tank Dimensions
Shell Length(ft): 50.00
Diameter(ft): 10.37
Volume(gallons): 31,590.00
Turnovers: 0.00
Net Throughput(gal/yr): 0.00
Is Tank Heated(y/n): N
Is Tank Underground(y/n): N
Paint Characteristics
Shell Color/Shade: Aluminum/Diffuse
Shell Condition Good
Breather Vent Settings
Vacuum Settings(psig): -0.25
Pressure Settings(psig) 0.75
Meterological Data used in Emissions Calculations:Raleigh,North Carolina(Avg Atmospheric Pressure=14.53 psia)
file:Z/C:\Prdgram Files\Tanks409d\summ4ry,"display..httn` i . :6/2/2014 _'

E , :'TAI�,?7'H.4.0 Report i _ u , ..; r t ,3 »� ,� �. �� E�� of6.
TANKS 4.0.9d
Emissions Report Detail format
is f z• Liquid Contents of Storage Tank
E9.30=Horizontal Tank:.
Now Hill; North Carolina'
Liquid
Daily Liquid-Surf. Bulk Vapor Liquid Vapor
Temperature(deg F) Temp Vapor Pressure(psia) Mol. Mass Mass Mol. Basis for Vapor Pressure
Mixture/Component Month Avg. Min.' Max. (deg F) Avg. Min. Max. Weight. Fract. Fract. Weight Calculations -
Purified Ethylene Glycol All 67.34 .57.58 77.10 61.88 0.0127 0.0088 0.0180 23.3652 60.59 .
Ethylene Glycol 0.0016 0.0010 0.0025 62.0690 i 0.9900 0.3226 62.07 Option 1:.VP60=.001095 VP70=.001774
Water 0.3312 0.2340 0A619 .18.0.150 .0:0100 016774 18.02 Option 1:VP60=.252846 VP70=.359616 . .
file:/1C:\Prog'ram Files\Tanks409d\su'nimarydf"splay.htm s i. : 6/2/2014.

TANF U Report _ - ;? i ;`� .- .; Fv 3 of 6
p TANKS 4.0.9d
r Emissions Report - Detail Format
> ( <. & Detail Calculations (AP-42)
E830-Horizontal Tank
New Hill, North Carolina .
Annual Emission Calcaulations
Standing Losses(lb): 0.2983
Vapor Space Volume(cu ft):' 2,689.7861
Vapor Density(lb/cult): 0.0001 _
Vapor Space Expansion Factor. 0.0058
Vented Vapor Saturation Factor. 6.9965'
Tank Vapor Space Volume:
Vapor Space Volume.(cu ft): 2,686.7861"
Tank Diameter(ft):" 10.3700
Effective Diameter(ft): 25.7004
Vapor Space Outage(ft): 5.1850
Tank Shell Length(ft): 50.0000
Vapor Density
Vapor Density(lb/cu ft): 0.0001
Vapor Molecular Weight(lb/lb-mole): 23.3652
Vapor Pressure at Daily Average Liquid
Surface Temperature(psia): 0.0127
Daily Avg.Liquid Surface Temp.(deg.R): 527.0125
Daily Average Ambient Temp.(deg.F):. 59.2833
Ideal Gas Constant R
(psia cult L(Ib-mol-deg R)): 10.731
Liquid Bulk Temperature(deg.R): 521.5533
Tank Paint Solar Absorptance(Shell): b.6000
Daily Total Solar Insulation "
Factor.(Btu/sgft day): 1,363.0797
Vapor Space Expansion Factor
Vapor Space Expansion Factor. 0.0058
Daily Vapor Temperature Range(deg.R): 39.0397
Daily Vapor Pressure Range(psia): 0.0091
Breather Vent Press:Setting Range(psia): 1.0000
Vapor Pressure at Daily Average Liquid
Surface Temperature(psia): 0.0127
Vapor Pressure at Daily Minimum Liquid.
Surface Temperature(psia): • 0.0086 .
Vapor Pressure at Daily Maximum Liquid
Surface Temperature(psia): 0.0180
Daily Avg.Liquid Surface Temp:(deg R): 527.0125
Daily Min.Liquid Surface Temp.(deg R): 517.2526
Daily Max.Liquid Surface Temp.(deg R): 536.7725
Daily Ambient Temp.Range(deg.R): 21.7167
Vented Vapor Saturation'Factor
Vented Vapor Saturation Factor; 0.9965
Vapor Pressure at Daily Average Liquid:
Surface Temperature(psia): 0.0127
Vapor Space.Outage'(ft): 5.1850
Working Losses(lb):- 0.0000
Vapor Molecular Weight(IbAb-mole): 23.3652
_Vapor Pressure at Daily Average Liquid
Surface Temperature(psia): 0.0127.'
Annual Net Throughput(gaVyr.): 0.00.00
i 6/2/2014 lle:HC:\Program,Files\Tanks409d\summarydisplay.htin .

TAIL'"" 4.0 Report. I, F, - 4 of 6 ; I
Annual Turnovers: 0.0000 .
Turnover Factor. 1.0000 8
Tank Diameter(ft): 10.3700
Working Loss Product Factor: 1.0000
Total Losses(Ib): 0.2983'.. .
'file://C�\Prograrn Files\Tanks409d\suinmarydisplay.htm i 6/2/2014 ;

rTAN7 C0 Report
TANKS 4:.0.9d
v ' Emissions Report;- Detail Format
Individual Tank Emission Totals:. t :
Emissions.Report for: Annual'
ES30=.Horizontal Tank.
New Hill, North Carolina
Losses(lbs)
Components Working Loss Breathing Loss Total Emissions
Purified Ethylene Glycol IF 0.00110:30 0.30 -
Ethylene Glycol =F 0.00 0.10 0.10
11
Water 0.00 0.20 0.20
6/2/2014
f le://C:\Program•Files\Tanks409d\summarydisplay.htin;: =' ; . f- ; ; i

TAT; ",4.0 Report . . F - §1:of;6)
f TANKS 4.0.9d
6 Emissions Report - Detail Format
1 s i Tank Indentification and Physical Characteristics
Identification
User Identification: Diesel Tank HT-8
City: Raleigh
State: North Carolina
Company: Performance Fibers
Type of Tank: Horizontal Tank
Description:
Tank Dimensions
Shell Length(ft): 12.00
Diameter(ft): 5.30
Volume(gallons): 2,000.00
Turnovers: 0.94
Net Throughput(gal/yr): 1,879.00
Is Tank Heated(y/n): N
Is Tank Underground(y/n): N
Paint Characteristics
Shell Color/Shade: Gray/Medium
Shell Condition Good
Breather Vent Settings
Vacuum Settings(psig): -0.03
Pressure Settings(psig) 0.03
Meterological Data used in Emissions Calculations:Raleigh,North Carolina(Avg Atmospheric Pressure=14.53 psia)
file://C:\Program Files\Tanks409d\summarydisplay.htni 1 6/2/2014 1 !

TAI�7":4.0 Report . , °I ;, _ i F�� '2.1 of 6i
TANKS 4.0.9d
Emissions Report - Detail Format
. ' Liquid Contents of Storage Tank-:. b f x r
Diesel.Tank HT-8 -Horizontal Tank r
Raleigh, North Carolina
Liquid
Daily'Liquid Surf. Bulk Vapor Liquid Vapor'
Temperature(deg F) Temp Vapor Pressure(psia)• Mol. Mass Mass Mol. Basis for Vapor Pressure
Mbdure/Component Month Avg. Min. Max. . (deg F) Avg. Min. _ Max. Weight. Fract Fract. Weight Calculations
Distillate fuel oil no.2 All- 68.49 57.95 79.03 62.36 0.0086 0.0061 0.0111 130.0000 188.00 Option 1:VP60=.0065 VP70=.009
fileM.Wrogra'rri Files\Tanks409d\§ummarydisplay.htm i, r. 6020141

�. TAI171'''.4.0 Report . . a . . 3 E of 6
TANKS'4.0.9d
Emissions Report - Detail.-Format
f Detail Calculations (AP42)
Diesel.Tank HT-8-Horizontal Tank i
Raleigh, North Carolina
Annual Emission Caloaulations
Standing Losses(lb): 0.9250
Vapor SpaceVolume(cu ft): 168.8255
Vapor Density(lb/cu ft): 0.0002
Vapor Space Expansion Factor. 0..0761
Vented Vapor Saturation Factor. 0.9988'
Tank Vapor Space Volume:
Vapor Space Volume(cu ft): 168.6255
Tank'Diameter(ft. 5.3000
Effective Diameter(ft): 9.0011
Vapor.Space Outage(ft): 2.6500
Tank Shell Length(ft): 12.0000'
Vapor Density
Vapor Density(lb/cu ft): 0.0002
Vapor Molecular,Weight(IbAb-mote); 130.0000
Vapor Pressure at Daily Average Liquid
Surface Temperature(psia): 0.0086
Daily Avg.Liquid Surface Temp.(deg.R): 528.1618
Daily Average Ambient Temp.(deg.F): 59.2833
Ideal Gas Constant R
(psia cult/(lb-mol-deg R)): 10.731
Liquid Bulk Temperature(deg.R): 522.0333
Tank Paint Solar Absorptance(Shell):. 0.6000
Daily Total Solar Insulation.
Factor(Btu/sgft day): 1;393.0797
Vapor Space Expansion Factor
Vapor Space Expansion Factor: 0.0761
.Daily Vapor Temperature Range(deg.R): 42.1602
Daily Vapor Pressure Range(psia): 0.0056-
Breather Vent Press.Setting Range(psia): 0.0600
Vapor Pressure at Daily Average Liquid
Surface Temperature(psia): 0.0086
Vapor Pressure at Daily Minimum Liquid
Surface Temperature(psia): 0.0061
Vapor Pressure at Daily Maximum Liquid
Surface Temperature(psia): 0.0117
Daily Avg..Liquid Surface Temp:(deg,R): 528.4618
Daily Min.Liq'uid'Surface Temp.(deg R): 517.6217
Daily Max.Liquid Surface Temp.(deg R): 638.7018
Daily Ambient.Temp.Range(deg.R): 21.7167
Vented Vapor Saturation Factor
Vented Vapor Saturation Factor: 0.9988
Vapor.Pressure at Daily Average Liquid:
Surface Temperature(psia): 0.0086
Vapor Space Outage(ft): 2.6500
Working Losses(lb): 0.0502.
Vapor Molecular Weight(lb/lb-mole): 130.0000 .
Vapor Pressure at Daily Average Liquid
Surface Temperature(psia): 0.0088
Annual Net Throughput(gallyr.): 1,879.0000
umm . %Z1° file \Program Files\Tanks409d\s m- /2014 v>

TAT`"'.4.0 Report _° 4- i :E. . 1
�, t I. T� ��4 of..b
Annual Turnovers: 0.9395
Turnover Factor: 1.0000
Tank Diameter(ft): 5.3000
Working Loss Product Factor: 1.0000
Total Losses(lb): 0.9752. ) + }
1
e fileWCAProgram Files\Tariks409d\summarydispldy..htm 6/2/2014 ) .

�z MS7> �L 4.0Report � � :a ' =F�� Si of 6 s t �
TANKS.4.0.9d r
Emissions Report' Detail Format
g Individual Tank Emission Totals_
Emissions Report for: Annual
Diesel Tank HT-8 -Horizontal Tank
Raleigh, North Carolina
Losses(lbs)
Components Working Lossil Breathing Loss . Total Emissioris
Distillate fuel oil no.2 0.05 0.93 1 0.98
7 i ifile://q:t\Program Files\Tanks409d\summarydisplay.htrri 7 ! f 6/2/20:14

TAN",4.0 Report ; . _ ! ? _. F7- 1 of 6
TANKS 4.0.9d
Emissions Report - Detail Format
:i ;Tank Indentification and Physical Characteristics
Identification
User Identification: VT-45
City: Raleigh
State: North Carolina
Company: Performance Fibers
Type of Tank: Vertical Fixed Roof Tank
Description: No.6 Fuel Oil Tank
Tank Dimensions
Shell Height(ft): 36.00
Diameter(ft): 33.75
Liquid Height(ft): 35.00
Avg.Liquid Height(ft): 24.00
Volume(gallons): 234,227.93
Turnovers: 0.00
Net Throughput(gaVyr): 624.00
Is Tank Heated(y/n): N
Paint Characteristics
Shell Coior/Shade: Gray/Medium
Shell Condition Good
Roof Color/Shade: Aluminum/Diffuse
Roof Condition: Good
Roof Characteristics
Type: Dome
Height(ft) 0.00
Radius(ft)(Dome Roof) 15.33
Breather Vent Settings
Vacuum Settings(psig): -0.03
Pressure Settings(psig) 0.03
Meterological Data used in Emissions Calculations:Raleigh,North Carolina(Avg Atmospheric Pressure=14.53 psia)
ay:htm fl'e://C:\Program Fi1es\Tdnks409d\summarydi9p1 t s ; . 6/2/2014 t

r TAY ",.4.0 Report P z 2W 6 1,
TANKS 4.0.9d '
•Emissions Report-' Detail-Format
$ liquid Contents of Storage,TAnk F r
VT-45-Vertical Fixed Roof Tank
Raleigh, North Carolina
Liquid
Daily Liquid Surf. Bulk Vapor Liquid Vapor
Temperature(deg F) Temp Vapor Pressure(psia) Mal. Mass' Mass Mal. Basis for Vapor Pressure
Mixture/Component Month Avg. Min. _ Max. (deg F) Avg. Min. Max. Weight. Fract. Fract. Weight Calculations -
Residual oil no.6 All 67.92 57.77 78.07 62.12 0.0001 0.0000 0.0001 190.0000 387.00 Option 1:VP60=.00004 VP70=.00006
f lea//C:\Program;Files\Tanks409d\summarydisplay.htm y z . r; 6/2/2014 i a

Report 4 IF' $tof 6
TANKS 4.0.9d
v Emissions:Report ' Detail Format
Detail-Ca 'lations (AP-42) r • .. . .
VT-45.-Vertical Fixed Roof Tank
Raleigh, North Carolina
Annual Emission Calcaulations
Standing Losses(lb):. 0.0000
Vapor Space Volume(cu ft): 0.0000
Vapor Density(lb/cu ft): 0.0000
Vapor Space Expansion Factor. 0.0728
Vented Vapor Saturation Factor. 1.0000'
Tank Vapor Space Volume:
Vapor Space Volume(cu ft): 0.0000-
Tank Diameter(ft): 33.7600
Vapor Space Outage(ft): 00000
Tank Shell Height(ft): 36.0000
Average Liquid Height(ft): 24.0000
Roof Outage(ft):. 0.0000
Roof Outage(Dome-Roof)
Roof Outage(ft): 0.0000
Dome Radius(ft): 15.3300
Shell Radius(ft): 16.8750
Vapor Density
Vapor Density(Ib/cu ft): 0.0000
Vapor Molecular Weight(Ib/Ib-mole): 190.0000
Vapor Pressure at Daily Average Liquid
Surface Temperature(psia): 0.0001
Daily Avg.Liquid Surface Temp.(deg.R): 527.5871
Daily Average Ambient Temp.(deg.F): 59.2833
Ideal Gas Constant R
(psia cult/(lb-mol-deg R)): .10.731
Liquid Bulk Temperature(deg.R): 521.7933 .
Tank Paint Solar Absorptance(Shell): 0.6800
Tank Paint Solar'Absorptance(Roof): 0.6000.
Daily Total Solar Insulation
Factor(Btu/sgft day): 1,393.0797
Vapor Space Expansion Factor
Vapor Space Expansion Factor. 0.0726
Daily Vapor Temperature Range(deg.R): 40.6000
Daily Vapor Pressure Range(psia): 0.0000
Breather Vent Press.Setting Range(psia): 0.0600
Vapor Pressure at Daily Average.Liquid
Surface Temperature(psia): 0.0001
Vapor Pressure at Daily Minimum Liquid
Surface Temperature(psia): 0.0000
Vapor Pressure at Daily Maximum Liquid
Surface Temperature(psia): 0.0001
Daily Avg.Liquid Surface Temp.(deg R): 527.5871
Daily Min.Liquid Surface Temp.(deg R): 517.4371 '
Daily Max.Liquid Surface Temp:(deg R): 537.7371
Daily Ambient Temp.Range(deg.,R): 21.7167
Vented Vapor Saturation Factor .
Vented Vapor Saturation Factor 1.0000
Vapor Pressure at Daily Average Liquid:
Surface Temperature(psia): 0.0001
Vapor Space Outage(ft): 0.0000
y' f le//C:\Program Files\Tanks4:09d\suminarydisplay.htm; l . '' ; ; : . r 16>2%2014 !

TAr7',CO Report \ , , _ � F 4'of 6.i
Working Losses(lb): 0.0002
Vapor Molecular Weight(lb/lb-mole):, 190.0000
Vapor Pressure at Daily Average Liquid
Surface Temperature(psia): 0.0001
Annual Net Throughput(galtyr.): 624.0000
-Annual Tumovers: - 0.0027.
Turnover Factor: 1.0000 .
Maximum Liquid Volume(gal): 234.227.9278
i Maximum Liquid.Height(ft): 35.0000
i > Tank Diameter(ft): 33.7500 }
Working Loss Product Factor: 1.0000
Total Losses(lb): 11.0002
b/2/2014
?file)/CAProgram Files\Tanks409d\siimmarydisplay.htm i i i

TAN,Y"_-CO Report, F�° 5 of 6 i
l
.TANKS 4.0.9d
Emissions Report- Detail Format
g £ I IndividualTank Emission Totals:..
Emissions Report for: Annual
VT-45-Vertical Fixed Roof Tank
Raleigh, North Carolina
Losses(lbs).
Components Working Loss Breathing Loss Total Emissions
Residual oil no.6 OM11 0.00 0.00
i� 3 p file://C.:\Program.Files\Tanks40gd\suipmarydi'splay.htm 6/2/2014 r ,

TANKS 4.0 Report Page 1 of 5
TANKS 4.0.9d
Emissions Report-Detail Format
Tank Indentification and Physical Characteristics
Identification ~
User Identification: HT-15
City: New Hill
State: North Carolina
Company: Performance Fibers,Inc.
Type of Tank: Horizontal Tank
Description: Unleaded Gasoline Tank
Tank Dimensions
Shell Length(it): 14.00
Diameter(it): 6.00
Volume(gallons): 971.00
Turnovers: . 2.06
Net Throughput(gal/yr): 2,002.00
Is Tank Heated(y/n): N
Is Tank Underground(y/n): N
Paint Characteristics
Shell Color/Shade: White/White
-Shell Condition "" Good
Breather Vent Settings
Vacuum Settings(psig): 0.00
Pressure Settings(psig) 0.00
Meterological Data used in Emissions Calculations:Raleigh,North Carolina(Avg Atmospheric Pressure=14.53 psia)
!
file://C:\Program Files\Tanks409d\summarydisplay.htm 6/2/2014

TANKS 4.0 Report Page 2 of 5
TANKS 4.0.9d. . . . .
Emissions Report-Detail Format
Liquid Contents.of Storage Tank
.HT-15-Horizontal Tank
New Hill,North Carolina
Liquid -
-- Daly Liquid Surf. Bulk Vapor Liquid Vapor
Temperature(deg F). Temp Vapor Pressure(psla) -Mol. Mass Mass _ MoL Bask for Vapor Pressure
NludrmpJComponerr( - Month Avg. Min. Max (deg F) Avg. Min. Max .WelghL F.6L Frect. Weight Calculations
Gasoline(RVP 15.0)' All 61.17 55.60 66.73 .59.30 8.3236 7.5132 92013 60.0060 92.00 _ Op6on 4:RVP=15,ASTM Sloped
2,2,4-Tdmethylpentane Qsaoctane) 0.6160 0.5240 0.7210 1142300 0.0303 0.0034 11423 Option 2:A=8.8118,8=1257.84,C-220.74.
Benzene 1.2081 1.0323 1.4035 78.1100 0.0303- 0,0067 78.11. Option 2:A=6.905,B=1211.033,C=220.79
EBrylberrzene 55
0.1130 0.0930 0.1367 106.1700 0.0242- 0.0005 106.17 Option 2:A=8.875,B=14242 ,Cy213.21
Hexane(-) - 1.9722 1.7044' 22736 86.1760 0.1394 0.0508 86.17 Option 2:A=8.876,6=1171.17.C-224.41
Naphthalene 0.0026 0.0020 0.0033 128.2000 0.0121 0.0000 12820 Option 2:A=7.3729,B=1968.38,C--M.61' _ -
Styrene - - 0.0748 0.0814 0.0906 104.1500 0.0061 0.0001 104.15 Option 2:A=7.14,B=1574.51;C=124,09
Toluene 0.3423 ,02874 0.4058 92.1300 0.1515 0.0096 92.13 Option 2:A=8.954,8=1344.8,C--219.48
Unidentified Components _ 15.5004 15.3693 15.3700 58.5484 OA970 0.9271 89.62
Xylenes(iNked Isomers) .. 0.0941 -0.0773 0.1141"108.1700 '0.1091 0.0019 108.17 Option 2:A-7.009,8=1462268,C=216.11.
file://C:\Program Files\Tanks409d\sumtnarydisplay.htrn 6/2/2014

TANK$n4.0 Report Page 3 of 5
TANKS 4.0.9d
Emissions Report-Detail Format
Detail Calculations(AP-42)
HT-15-Horizontal Tank
New Hill;North Carolina
Annual Emission Cal aulatims- - -
Standing Losses Qb): 1,114.1075
VeporSpace Volume(m ft): 252.1278
Vapor Density Qb/cu ft): 0.0894 - -
Vapor Spare Expansion Factor. 0.3148,
Vented Vapor Saturation Factor. 0.4304
Tank Vapor Spam Volume:.
Vapor Spam Volume(cu ft): . . 252.1278
Tank Diameter(It): 6.0000 - - - - - -
Effective Diameter(ft): 10.3444 -
.Vapor Spam Outage(it): 3.0000 .. .. ..
Tank Shell Length(it):_ 14.0000
Vapor Density ..••. - - -
Vapor Density(m/ce ft): 0.0894 -
Vapor Molecular Weight Qb9G-file): 60.0000 -
a!BSurtaPor.Precessuggt D$%Awrage Liquid
" . Temperatora(psla):. 8.3238 .
Deily Avg.Llquld SuRace Temp.(deg.R): 520.8354 - -
Dely AVerage Ambient Temp.(deg:F): 69.2833
Ideal Gas Constant .. .. .. ..
(psia cut/Qbmol4eg R)): 10.731
Liquid Bulk Temperature(deg.R): 51".9733 - - -
Tank Paint SolwAbsorptance(Shen): 0.1700 ,
Daly Total Solar Insulation. -
Factor(BadsgR day): .. - 1,393.0797
Vapor Space.Expansion Factor
Vapor Spam Expansion Factor. 0.3148
Daly Vapor Temperature Range(deg.R): 22.2671
..Daly Vapor Pressure Range(psis): 1.8881
Breather Vent Press.Selling Range(psia): 0.0000
Vapor Pressure at Daily Average Liquid -
,Surface Temperature(psia): 8.3238 -
Vapor Pressure at Daily Minimum Liquid
Surface Temperature(paid):" - 7.5132"
Vapor Pressure at Dalyy Maximum Liquid - -
Surface Temperature(psla):.- 9.2013 -
Daily Avg.liquid Surface Temp.(deg R): 620.8354
Daly Mn.Liquid Surface Temp.(deg R): 515.2687 - -
.Dalyax.M Liquid Surface Temp.(deg R): 526.4022 -- "
Daly Ambient Temp.Range(deg.R): 21.7167
Vented Vapor Saturation Factor
Vented Vapor Saturation Factor. 0.4304 -
Vapor Pressure at Daily Average Liquid: -
Surface Temperature(psia): 8.3238 Vapor.Spam Outage(it):, - 3.0000
Working Losses.Qb):,-. 23.8054
L_= Vapor Moecular Welght Qbllb-mole): 60.0000 -
Vapor Pressure at Daily Average Liquid
Surface Temperature(psia): - 8.3236 -
Annual Net Throughput(9allyr.): 2,002'0000 - -
Annual TumoVere: - 2.0818
�Tumover Factor. 1.0000 -
Tank Diameter(it): 6.0000 -
Working Loss Product Factor. 1:0000
Total Losses(Ib): '1,137.9129 -
fileWCAProgram Files\Tanks409d\suminarydisplay.htrn 6/2/2014

TANKSAP:O eport Page 4 of 5
TANKS 4.0.9d
Emissions Report-Detail Format
Individual Tank Emission.Totals
Emissions Report for:Annual
HT-15-Horizontal Tank
New Hill,NbAh Carolina
Losses(lbs)
Components Wanking Loss Breathing Loss Total Emissions
Gasoline.(RVP 15.0) - _ 23.81]F 1,114.1111. 1,137.91
Toluene . 0.23 10:64 10.87
Xylenes(m ned isomers) 0.05 2.11 2.15
Hexane(-n) 1.21 56.42 57.63 ..
Benzene 0,1611 7.66
2,2,4-Trimethylpentane(isooctane)- 0.08 3.83L 3.91
Ethylbeniene . 0.0111. 0:56 0.57
Naphthalene 0.00 1 0.01
Styrene. 0.00 0.09 0.10
Unidentified Components 22.07 1,032.94 1;055.01
file://CAProgram Files\Tanks409d\summarydisplay.httn 6/2/2014