RE:ATTACHMENT ATTACHMENT ATTACHMENT:Additional Info Needed for MCU AAQIR Additional Info Needed for MCU AAQIR

Dwight Mallory Dwight Mallory to: Andrew Chew 12/04/2012 11:38 AM

Cc: Shaheerah Kelly

History: This message has been replied to.

Andrew,

In the attached Word document you will find a list of the questions 

from your October 30 email, followed by a brief response to each one. 

The attached Xcel file includes a summary worksheet with the 

individual emissions unit and facility-wide actual and PTE emissions 

estimates. Also attached are pdf files with the GLYCalc input and 

aggregate reports for the dehydrator PTE and 2011 actual emissions, as 

well as pdf prints of the EPA Tanks reports for the gasoline storage 

tank. 

I apologize for running a few days beyond the one-month response 

time we discussed. For reasons explained in the attachments, I ended 

up having to revisit the Main Flare tons per year PTE figures submitted 

with the 2008 PSD application and it took a bit longer than I 

anticipated. 

I spoke with Tom Hormel at McVehil-Monnett yesterday concerning 

the Level II modeling that Don Shepherd at NPS requested. He said he 

has finished the modeling and should get the final report out to Mr. 

Shepherd and the rest of us in the next week. 

I’ll touch base with you when the modeling report gets here. In the 

meantime, let me know if you need anything else.

Dwight E. Mallory

Environmental, Health & Safety Coordinator

Resolute Energy Corporation

1675 Broadway, Suite 1950

Denver, CO 80202

Direct: 303-573-4886 X 1165

Cell: 970-302-8620

Email: dmallory@ResoluteEnergy.com

From: Chew.Andrew@epamail.epa.gov [

mailto:Chew.Andrew@epamail.epa.gov] 

Sent: Tuesday, October 30, 2012 10:33 AM

To: Dwight Mallory

Cc: Kelly.Shaheerah@epamail.epa.gov

Subject: ATTACHMENT: Additional Info Needed for MCU AAQIR

Hi Dwight,
Shaheerah is peer-reviewing my write-up for the draft flare permit and we 

need the following information available when we are ready to public 

notice the permit. Hope it works for you if we can get the information 

from you within a month's timeframe. Also, can you let me know how 

things are going with the modeled impacts for Hovenweep that Don 

Shepherd at the National Park Service asked for? Thanks again for your 

help.

- Andrew 

 -------------------------------------------

Andrew Chew, P.E. 

T: (415) 947-4197 | F: (415) 947-3579 | chew.andrew@epa.gov

U.S. EPA, Region 9, Air Permits Office (AIR-3) | 75 Hawthorne St., San 

Francisco, CA 94105

----- Forwarded by Andrew Chew/R9/USEPA/US on 10/30/2012 09:23 AM -----

From: Shaheerah Kelly/R9/USEPA/US

To: Andrew Chew/R9/USEPA/US@EPA

Date: 10/29/2012 12:14 PM

Subject: Additional Info Needed for MCU AAQIR

Hi Andrew,

Here is the additional info that is needed to fill in some of the gaps for the 

MCU AAQIR PSD permit amendment. It would be very helpful if you 

could get this info from Resolute and find out if the company can provide 

this info within the next month or so. Thanks.

1) Provide facility-wide actual emissions and PTE estimates for SO2, 

CO, NOX, VOC, PM, PM10. and PM2.5. Section 3 of the 2008 PSD 

application provides emissions info for the Main Flare only. 

2) Provide actual emissions and PTE estimates for SO2, CO, NOX, 

VOC, PM, PM10. and PM2.5 for the following emission units. Section 3 

of the 2008 PSD application provides emissions info for the Main Flare 

only. 

 TEG Reboiler (0.33 MMBtu/hr) - Operational

 Main Flare (618,104 scf/hr) - Operational

 Gasoline Storage Tank (1000 gallons) - Operational

 Glycol Heater (rated size/capacity?) - Operational

3) Verify the accuracy of the rated sizes/capacities of the following 

emission units, and provide the rated sizes/capacities where none is 

identified.

 TEG Reboiler (0.33 MMBtu/hr) - Operational

 Main Flare (618,104 scf/hr) - Operational
 Gasoline Storage Tank (1000 gallons) - Operational

 Glycol Heater (rated size/capacity?) - Operational

4) Verify the accuracy of the following information regarding the

operational status of (i) the emissions units listed in the current PSD 

permit and (ii) the other operations at the MCU facility.

Equipment in current MCU Facility PSD Permit lasted amended in 1991:

 T4500 Gas Turbine (4390 HP) - Shutdown 1997

 Waste Heat Recovery Unit (11 MMBtu/hr) - Shutdown 1997

 Ingersoll Rand IC Engine (491 HP) - Shutdown 1993

 Fairbanks Morse IC Engine (1712 HP) - Shutdown 1997

 Fairbanks Morse IC Engine (1712 HP) - Shutdown 1997

 Fairbanks Morse IC Engine (1848 HP) - Shutdown 1997

 Fairbanks Morse IC Engine (1848 HP) - Shutdown 1997

 DPC-540 IC Engine (470 HP) - Shutdown 1998

 HC Liquid Reboiler (1 MMBtu/hr) - Shutdown 1993

 Heat Medium Heater (4 MMBtu/hr) - Shutdown 1993

 Heat Medium Heater (12.2 MMBtu/hr) -Shutdown 1991

 TEG Reboiler (0.33 MMBtu/hr) - Operational

 TEG Reboiler (0.33 MMBtu/hr) - Shutdown 1991

 TEG Reboiler (0.33 MMBtu/hr) - Shutdown 1991

 TEG Reboiler (0.1 MMBtu/hr) - Shutdown 1991

Other Operations at the MCU Facility:

 Natural Gas Liquids Processing - Shutdown 1998

 Natural Gas Processing Facility - Shutdown 1998

 Main Flare (618,104 scf/hr) - Operational

 Gasoline Storage Tank - Shutdown 1993

 Gasoline Storage Tank - Shutdown 1993

 Gasoline Storage Tank (1000 gallons) - Operational

 Diesel Storage Tank - Shutdown 1993

 CO2 line heater - Shutdown 2004

 Glycol Heater - Operational

5) EPA was provided the attached description of the MCU facility by 

Mobil in the past. Please verify the accuracy of this information and 

clarify whether it is acceptable to use this description as part of the PSD 

application

************************************

Shaheerah Kelly, Environmental Engineer

U.S. Environmental Protection Agency, Region 9

Permits Office, Air Division 

San Francisco, CA 94105

Phone: 415-947-4156

Fax: 415-947-3579
Email: kelly.shaheerah@epa.govResponse to 10-30-12 Questions.docx

Revised Facility Emissions.xlsx MCU_DEHY_PTE_Input.pdf

Fuel Tank 2011 Est.pdf Fuel Tank PTE.pdf MCU_DEHY_2011.pdf

MCU_DEHY_2011_Input.pdf MCU_DEHY_PTE.pdf
1) Provide facility-wide actual emissions and PTE estimates for SO2, CO, NOX, VOC, PM, PM10 and 

PM2.5. Section 3 of the 2008 PSD application provides emissions info for the Main Flare only. 

Estimates of facility-wide PTE, as well as actual emissions for the most recent 5 year 

period, are included in the attached spreadsheet. Note that the PTE estimates for the Main 

Flare have been revised from the figures submitted in the 2008 PSD application. The 

reason for the revision is that the actual volume of gas combusted in the main flare in 

calendar year 2008, as well as the resulting emissions, exceeded the PTE values submitted 

in the 2008 application for NOx, CO and VOC. 

The revised PTE estimates were derived using the same calculation methods, heat content 

and H2S concentration values specified in the 2008 PSD application. However, the PTE 

volume of gas combusted in the Main Flare was revised from 1,070,366 kscf per year in the 

2008 PSD application to 1,263,857 kscf per year. 

The 2008 PTE flare volume was derived using the actual volume of gas combusted in the 

Main Flare during calendar year 2003. The 2003 volume, which was at that time the 

maximum annual volume of gas combusted in the Main Flare, was adjusted upward by 

20% and the resulting gas volume was applied to the assumed maximum gas heat content 

and H2S concentration values to determine the PTE for SO2, VOC, CO, NOx and PM. 

The 2012 revised PTE flare volume was derived using the 2008 actual volume of gas 

combusted in the Main Flare. The 2008 Main Flare volume is the maximum volume of gas 

combusted in the Main Flare and includes gas combusted during a complete emergency 

shutdown of the facility that was caused by corrosion related equipment failures. The 

facility shut down, which lasted for several weeks, required all of the process gas received 

at the facility to be flared and provided real-life worst-case scenario upon which the revised 

PTE figures are based. Because the 2008 Main Flare gas volume includes gas combusted 

during the extended facility shut down, the 2008 actual volume was only adjusted upward 

by 10% for PTE determination. 

The PTE revision affects only the potential volume of gas combusted in the Main Flare on 

an annual basis and the resulting tons per year PTE figures. The maximum heat content 

and H2S concentration assumptions, calculation methods and short term maximum 

emission rates from the 2008 application remain valid. 

2) Provide actual emissions and PTE estimates for SO2, CO, NOX, VOC, PM, PM10 and PM2.5 for the 

following emission units. Section 3 of the 2008 PSD application provides emissions info for the Main Flare 

only. 

 TEG Reboiler (0.33 MMBtu/hr) - Operational 

 Main Flare (618,104 scf/hr) - Operational 

 Gasoline Storage Tank (1000 gallons) - Operational 

 Glycol Heater (rated size/capacity?) – Operational

PTE and actual emissions estimates for each of the listed emissions units are included in the 

attached spreadsheet.
3) Verify the accuracy of the rated sizes/capacities of the following emission units, and provide the rated 

sizes/capacities where none is identified. 

 TEG Reboiler (0.33 MMBtu/hr) - Operational 

 Main Flare (618,104 scf/hr) - Operational 

 Gasoline Storage Tank (1000 gallons) - Operational 

 Glycol Heater (rated size/capacity?) – Operational

The design information in the files at the facility indicates that the TEG Reboiler (TEG 

Regenerator Heater) remaining in use at the site has an actual rating of 0.75 MMBtu/hr 

and not 0.33 MMBtu/hr. 

The Main Flare rating of 618,104 scf/hr is correct. 

The remaining gasoline storage tank is 10,000 gallons nominal capacity (9,925 gal actual) 

and not 1,000 gallons. 

The Glycol Heater (TEG Regenerator Vent) has a maximum throughput of 12 MMCFD. 

However, the current facility configuration limits dehydrator throughput to output from 

the HOS-6 compressor, which is approximately 6 MMCFD. 

4) Verify the accuracy of the following information regarding the operational status of (i) the emissions 

units listed in the current PSD permit and (ii) the other operations at the MCU facility. 

Equipment in current MCU Facility PSD Permit lasted amended in 1991: 

 T4500 Gas Turbine (4390 HP) - Shutdown 1997 

 Waste Heat Recovery Unit (11 MMBtu/hr) - Shutdown 1997 

 Ingersoll Rand IC Engine (491 HP) - Shutdown 1993 

 Fairbanks Morse IC Engine (1712 HP) - Shutdown 1997 

 Fairbanks Morse IC Engine (1712 HP) - Shutdown 1997 

 Fairbanks Morse IC Engine (1848 HP) - Shutdown 1997 

 Fairbanks Morse IC Engine (1848 HP) - Shutdown 1997 

 DPC-540 IC Engine (470 HP) - Shutdown 1998 

 HC Liquid Reboiler (1 MMBtu/hr) - Shutdown 1993 

 Heat Medium Heater (4 MMBtu/hr) - Shutdown 1993 

 Heat Medium Heater (12.2 MMBtu/hr) -Shutdown 1991 

 TEG Reboiler (0.33 MMBtu/hr) - Operational 

 TEG Reboiler (0.33 MMBtu/hr) - Shutdown 1991 

 TEG Reboiler (0.33 MMBtu/hr) - Shutdown 1991 

 TEG Reboiler (0.1 MMBtu/hr) - Shutdown 1991 

Other Operations at the MCU Facility: 

 Natural Gas Liquids Processing - Shutdown 1998 

 Natural Gas Processing Facility - Shutdown 1998 

 Main Flare (618,104 scf/hr) - Operational 

 Gasoline Storage Tank - Shutdown 1993 

 Gasoline Storage Tank - Shutdown 1993 

 Gasoline Storage Tank (1000 gallons) - Operational 
 Diesel Storage Tank - Shutdown 1993 

 CO2 line heater - Shutdown 2004 

 Glycol Heater - Operational

This information appears to be correct, with the exception of the previously corrected 

ratings and capacities. For further clarification, the emissions units still in operation at the 

facility include: 

1) One (1) Main Flare, rated at 618,104 scf/hr, which combusts produced field gas in 

excess of the facility compression capacity 

2) One (1) TEG Reboiler rated at 0.75 MMBtu/hr, which combusts purchased pipeline 

quality natural gas to provide heat to the Glycol Heater. 

3) One (1) Glycol Heater (TEG regenerator), rated at 12 MMCFD, which provides 

inter-stage dehydration for the HOS-6 compressor. 

4) One (1) 10,000 gallon nominal capacity gasoline storage tank that is used for 

refueling of vehicles. 

5) EPA was provided the attached description of the MCU facility by Mobil in the past. Please verify the 

accuracy of this information and clarify whether it is acceptable to use this description as part of the PSD 

application 

The information is the attachment appears to be materially correct. However, use of the 

Paragraph A, “Field Process” description in the PSD permit application might be 

somewhat misleading in that the facility for which the PSD permit is being applied does not 

include the wells or oil production facilities described in this section. The PSD facility 

includes only the plant, which is comprised of the equipment and processes listed in the 

response to question 4 and discussed in Paragraph B, “Plant and Process Overview” of the 

attachment. 
2007 ‐2011 Actual Emissions and PTE Estimate

Volume SO2 NOx CO VOC PM Volume SO3 NOx CO VOC PM SO2 NOx CO VO

MMCF TPY TPY TPY TPY TPY MMCF TPY TPY TPY TPY TPY TPY TPY TPY TPY 

2007 640.4 16.8 12.7 69.2 83.9 1.4 1,750.0 0.0 0.1 0.5 2.9 0.0 0.0 0.3 0.3 0.0 2008 1,203.7 21.0 25.1 136.5 163.9 2.8 1,750.0 0.0 0.1 0.5 2.9 0.0 0.0 0.3 0.3 0.0 2009 416.0 19.3 8.3 45.4 52.3 0.9 1,750.0 0.0 0.1 0.5 2.9 0.0 0.0 0.3 0.3 0.0 2010 289.4 12.8 5.8 31.5 38.2 0.6 1,729.0 0.0 0.1 0.5 2.9 0.0 0.0 0.3 0.3 0.0 2011 423.4 26.7 8.4 45.4 54.9 0.9 1,598.1 0.0 0.1 0.5 2.7 0.0 0.0 0.3 0.3 0.0 

PTE 1,324.0 76.5 30.7 167.2 188.4 3.4 4,380.0 0.0 0.1 0.5 7.3 0.0 0.0 0.3 0.3 0.0 

McElmo Creek Unit Central Compression and Reinjection Facility

Regenerator Heater emissions from natural gas combustion were calculated using emissions factors from AP-42, Chapter 1, Table 1.4-1 and Tawas assumed to be operating at its maximum rated capacity 8,760 hrs per year. Gasoline storage tank PTE and actual emissions include working and standing emissions, which were estimated using EPA Tanks Version 4.0.942 Section 5.2 emissions factors. Because itemized fuel invoices for the MCU tank were unavailable, annual gasoline throughput was estimated estimated fuel economy of fleet vehicles. Because annual mileage records for previous years were unavailable, 2011 actual emissions were use

Main Flare 

(618,104 scf/hr)

PTE estimates for the Main Flare have been revised from the figures submitted in the 2008 PSD application. The 2012 revised PTE estimates wassumptions specified in the 2008 PSD application. While the calculation methods and gas composition assumptions from the 2008 application 1,070,366 kscf per year in the 2008 PSD application update to 1,263,857 kscf per year. This revision reflects a change in the maximum actual flThe 2008 PTE flare volume was derived using the actual volume of gas combusted in the Main Flare during calendar year 2003. The 2003 voluFlare, was adjusted upward by 20% and the resulting gas volume was applied to the maximum gas heat content and H2S concentration values volume was derived using the 2008 actual volume of gas combusted in the Main Flare. The 2008 Main Flare volume is the maximum volume of during a complete emergency shut down of the facility that was caused by corrosion related equipment failures. The facility shut down, which lasflared and provided an actual worst-case scenario upon which the revised PTE figures are based.. Because the 2008 Main Flare gas volume incwas only adjusted upward by 10% for PTE determination. 

Year 

Main Flare actual emissions for 2007 through 2011 were estimated using the calculation methods and site specific monthly gas composition as 2-1-2237, filed June 8, 2005) included as Appendix A to the 2008 PSD application. 

Glycol Heater (Regenerator Vent) 

(12 mmscf/day)

TEG Reboiler 

(0.75 mmbtu/hr)

Calculation Notes: Regenerator Vent VOC emissions were estimated using GRI-GLYCalc Version 4.0. Actual emissions for 2010 and 2011 were estimated using aActual dehydrator gas throughput for 2007 through 2009 was not measured, so actual emissions for these years was determined using a conse12 MMCFD gas throughput and using the actual site specific gas analysis and glycol circulation data. Dehydrator flash gas and regenerator emiassume 95% VOC destruction efficiency. Regerator Vent NOx, CO and SO2 values reflect emissions from the Main Flare as a result of the dehy

Revised November 2012
McElmo Creek Unit Main Flare

Actual Emissions 2007 ‐ 2011

Date Volume Flared SO2 NOx CO VOC PM

2007 Calendar Year Totals

(MMCF and TPY)

Date Volume Flared SO2 NOx CO VOC PM

2008 Calendar Year Totals

(MMCF and TPY)

Date Volume Flared SO2 NOx CO VOC PM

2009 Calendar Year Totals

(MMCF and TPY)

Date Volume Flared SO2 NOx CO VOC PM

2010 Calendar Year Totals

(MMCF and TPY)

Date Volume Flared SO2 NOx CO VOC PM

2011 Calendar Year Totals

(MMCF and TPY)

Main Flare PTE Revision

V ‐ Flare Volume (kscf/yr) GHV MWSO2 MWVOC MFH2S WFVOC ERVOC ERSO2 

1,324,040 682.4 64.0 37.3 0.0 0.145 188.4 76.5 

EFNOx 0.068 lbs/mmbtu

EFCO 0.37 lbs/mmbtu

EFPM 0.00745 lbs/mmbtu

Input Values (see Appendix B of 2008 PSD Application) Emissions 

1,204 163.9 21.0 25.1 136.5

289 38.2 12.8 5.8 31.5

416 52.3 8.3 45.4640 83.9 16.8 12.7 69.2

19.3

1.42.80.90.6

423 54.9 26.7 8.4 45.4 0.9
Source: MCU TEG Reboiler 

Emission Calculation for External Combustion Sources

(For Estimating Emissions, Using Emission Factors from EPA AP-42, Table 1.4-1 and Table 1.4-2)

Burner Data

Reference Burner Annual Fuel Fuel Htg Fuel

No. Equipment Rating Op Time Type Value Use

(MMBtu/Hr) (hours) (Btu/scf) (MMSCF/Year)

Fuel Use (MMSCF/Year) = Burner Rating (MMBtu/Hr) * 106 Btu/MMBtu * Operating Hours * 1 scf/1,020 Btu * 1 MMBtu/106 Btu

Emission Factors

Reference Burner

No. Rating SO2 NOx CO VOC PM1

(MMBtu/Hr) (Lbs/106

 scf) (Lbs/106 scf) (Lbs/106 scf) (Lbs/106 scf) (Lbs/106 scf)

Regenerator 0.750 0.6 100.0 84.0 5.5 7.6

AP-42 AP-42 AP-42 AP-42 AP-42 1

Per AP-42 Table 1.4-2: All PM is assumed to be less than 1.0 micrometer in diameter. Therefore, the listed PM emission factor is used used to estimate PM10, PM2.5 and PM1

Reference

No. SO2 NOx CO VOC PM1

TPY TPY TPY TPY TPY

Regenerator 0.002 0.32 0.27 0.02 0.02

AP-42 Calculation Method

EF Source

Emission Factors

1,020 6.4

Source Emissions

Source Emissions

Regenerator Direct Fired TEG Reboiler 

Heater 0.75 8,760 Natural Gas
Facility Name: MCU Main Flare Emissions From Dehy Control

(Based on Office of Air Quality Planning and Standards, EPA, AP-42 Manual, Fifth Edition, January 1995, Section 13.5)

Annual Hours of Operation 8,760

Source with vapors sent to the 

Combustion Chamber Note

Vapor 

Volume 

(scf/hr)

Vapor 

Heating 

Value 

(btu/scf)

H2S 

Content 

(%)

NOx (lb/hr) NOx (Tons Per Year) CO (lb/hr) CO (Tons Per Year) SO2 (lb/hr) SO2 (Tons Per Year)

Flash Tank Off Gas 1,2 67 443.2 0.00 0.00 0.01 0.01 0.05 0.00 0.00Regenerator Vent 1,2 879 248.0 0.00 0.01 0.06 0.08 0.35 0.01 0.03Supplemental Fuel 1,2 55 1,020.0 0.00 0.00 0.02 0.02 0.09 0.00 0.00

Total 1,001 0.02 0.09 0.11 0.49 0.01 0.03

NOTES: 1 - Flare NOx and CO emissions based on continuous operation, using emission factors from AP42, Chapter 13-5 

2 - Flare VOC emissions based on 95% destruction efficiency of the control equipment.3 - VOC and HAP emissions accounted for in GRI-GLYCalc simulations4 - Flash Tank Off Gas and Regenerator Vent volume and composition were derived from GLYCalc stream reports5 - Supplemental Fuel Requirement derived from GLYCalc Equipment Reports

Dehydrator Control Flare Emission Analysis Worksheet

Lesair Environmental, Inc.www.lesair.com
Facility Name: MCU Flare Emissions From Dehydrator Control

(Based on Office of Air Quality Planning and Standards, EPA, AP-42 Manual, Fifth Edition, January 1995, Section 13.5)

Annual Hours of Operation 8,760

Source with vapors sent to the 

Combustion Chamber Note

Vapor 

Volume 

(scf/hr)

Vapor 

Heating 

Value 

(btu/scf)

H2S 

Content 

(%)

NOx (lb/hr) NOx (Tons Per Year) CO (lb/hr) CO (Tons Per Year) SO2 (lb/hr) SO2 (Tons Per Year)

Flash Tank Off Gas 1,2 67 443.4 0.00 0.00 0.01 0.01 0.05 0.00 0.00Regenerator Vent 1,2 879 273.3 0.01 0.02 0.07 0.09 0.39 0.01 0.03Supplemental Fuel 1,2 55 1,020.0 0.00 0.00 0.02 0.02 0.09 0.00 0.00

Total 1,001 0.02 0.10 0.12 0.53 0.01 0.03

NOTES: 1 - Flare NOx and CO emissions based on continuous operation, using emission factors from AP42, Chapter 13-5 

2 - Flare VOC emissions based on 95% destruction efficiency of the control equipment.3 - VOC and HAP emissions accounted for in GRI-GLYCalc simulations4 - Flash Tank Off Gas and Regenerator Vent volume and composition were derived from GLYCalc stream reports5 - Supplemental Fuel Requirement derived from GLYCalc Equipment Reports

Dehydrator Control Flare Emission Analysis Worksheet

Lesair Environmental, Inc.www.lesair.com
AP-42 Section 5.2 Transportation And Marketing Of Petroleum Liquid

s

Refueling Losses= 11 lbs/10^3 Gal. Emissions Factor from AP42 Table 5.2-7

Load Volume = 333 Gal/PD

4 lbs/Day

1335.9 lbs/Yr

Spillage Losses= 1 lbs/10^3 Gal. Emissions Factor from AP42 Table 5.2-7

Load Volume = 333 Gal/PD

0 lbs/Day

85.0 lbs/Yr

Total Refueling Losses 1420.9 lbs/Yr

EPA Tanks 4.0.9d Emissions Report for MCU Fuel Tank Working and Breathing Losses: Annual 

MCU Fuel 1 - Horizontal TankAneth, Utah

Components Working Loss Breathing Loss Total EmissionsGasoline (RVP 10) 898.48 1,742.05 2,640.52

4,061 lbs/yr

2.0 TP

Y

MCU Bulk Gasoline Tank Estimated Annual Fuel Throughput

Total Units Total Miles Miles/Unit MCU Units MCU Miles Avg MPG1 MCU Gallons

Aug-11 102 146,999 1,441 73 105,205 14 7,515

Sep-11 103 161,294 1,566 73 114,315 14 8,165

Oct-11 105 169,049 1,610 73 117,529 14 8,395

Nov-11 105 167,565 1,596 73 116,498 14 8,321Dec-11 97 160,605 1,656 73 120,868 14 8,633

Jan-12 93 170,714 1,836 73 134,001 14 9,572

50,601

MCU Avg Monthly Fuel Use 8,434 ga

MCU Annualized Fuel Use for PTE 121,443 ga

Avg MPG is the EPA "City" mileage rating for the 2010 Ford F-150 4X4, which is the std fleet vehicle used by RNRCEstimated fuel use for the MCU gasoline storage tank was determined using the most recent 6 months of actual vehicle mileage that were available. The averagmiles per vehicle was multiplied by the number of units assigned to the facility to estimate the total miles attributable to the facility. The total number of miles wadivided by the estimated average fuel economy of the fleet to estimate the gallons of fuel used. The fuel gallons used was increased by 20% for PTE estimation

EVAPORATIVE EMISSIONS FROM GASOLINE SERVICESTATION OPERATIONS (Table 5.2-7)

VOC Emissions =VOC Emissions =

Losses(lbs)

Total VOC Emissions from MCU Gasoline Stoage/Refueling Tank (Refueling 

Losses + Working and Standing Losses)
AP-42 Section 5.2 Transportation And Marketing Of Petroleum Liquid

s

Refueling Losses= 11 lbs/10^3 Gal. Emissions Factor from AP42 Table 5.2-7

Load Volume = 333 Gal/PD

4 lbs/Day

1335.9 lbs/Yr

Spillage Losses= 1 lbs/10^3 Gal. Emissions Factor from AP42 Table 5.2-7

Load Volume = 333 Gal/PD

0 lbs/Day

85.0 lbs/Yr

Total Refueling Losses 1420.9 lbs/Yr

EPA Tanks 4.0.9d Emissions Report for MCU Fuel Tank Working and Breathing Losses: Annual 

MCU Fuel 1 - Horizontal TankAneth, Utah

Components Working Loss Breathing Loss Total EmissionsGasoline (RVP 10) 748.73 1,742.05 2,490.77

3,912 lbs/yr

2.0 TP

Y

MCU Bulk Gasoline Tank Estimated Annual Fuel Throughput

Total Units Total Miles Miles/Unit MCU Units MCU Miles Avg MPG1 MCU Gallons

Aug-11 102 146,999 1,441 73 105,205 14 7,515

Sep-11 103 161,294 1,566 73 114,315 14 8,165

Oct-11 105 169,049 1,610 73 117,529 14 8,395

Nov-11 105 167,565 1,596 73 116,498 14 8,321Dec-11 97 160,605 1,656 73 120,868 14 8,633

Jan-12 93 170,714 1,836 73 134,001 14 9,572

50,601

MCU Avg Monthly Fuel Use 8,434 ga

MCU Annualized Fuel Use for PTE 121,443 ga

Avg MPG is the EPA "City" mileage rating for the 2010 Ford F-150 4X4, which is the std fleet vehicle used by RNRCEstimated fuel use for the MCU gasoline storage tank was determined using the most recent 6 months of actual vehicle mileage that were available. The averagmiles per vehicle was multiplied by the number of units assigned to the facility to estimate the total miles attributable to the facility. The total number of miles wadivided by the estimated average fuel economy of the fleet to estimate the gallons of fuel used. The fuel gallons used was increased by 20% for PTE estimation

EVAPORATIVE EMISSIONS FROM GASOLINE SERVICESTATION OPERATIONS (Table 5.2-7)

VOC Emissions =VOC Emissions =

Losses(lbs)

Total VOC Emissions from MCU Gasoline Stoage/Refueling Tank (Refueling 

Losses + Working and Standing Losses)
MCU Bulk Gasoline Tank Estimated Annual Fuel Throughput

Total Units Total Miles Miles/Unit MCU Units MCU Miles Avg MPG MCU Gallons

Aug‐11 102 146,999 1,441 73 105,205 14 7,515

Sep‐11 103 161,294 1,566 73 114,315 14 8,165

Oct‐11 105 169,049 1,610 73 117,529 14 8,395

Nov‐11 105 167,565 1,596 73 116,498 14 8,321

Dec‐11 97 160,605 1,656 73 120,868 14 8,633

Jan‐12 93 170,714 1,836 73 134,001 14 9,572

50,601

MCU Avg Monthly Fuel Use 8,434 gal

MCU Annualized Fuel Use for 2011 Emissions 101,202 gal

MCU Annualized Fuel Use for PTE 121,443 gal

Avg MPG is the EPA "City" mileage rating for the 2010 Ford F‐150 4X4, which is the std fleet vehicle used by RNRC

Estimated fuel use for the MCU gasoline storage tank was determined using the most recent 6 months of actual vehicle mileag

were available. The average miles per vehicle was multiplied by the number of units assigned to the facility to estimate the to

miles attributable to the facility. The total number of miles was then divided by the estimated average fuel economy of the fle

estimate the gallons of fuel used. The fuel gallons used was increased by 20% for PTE estimation.
TANKS 4.0.9d

Emissions Report - Detail Format 

Tank Indentification and Physical Characteristics

Identification

 User Identification: MCU Fuel 1

 City: Aneth

 State: Utah

 Company: Resolute

 Type of Tank: Horizontal Tank

 Description: 1,000 gal Fuel Tank at MCU Central Facility

Tank Dimensions

 Shell Length (ft): 26.40

 Diameter (ft): 8.00

 Volume (gallons): 9,932.00

 Turnovers: 10.19

 Net Throughput(gal/yr): 101,202.00

 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): -0.03

 Pressure Settings (psig) 0.03

Meterological Data used in Emissions Calculations: Grand Junction, Colorado (Avg Atmospheric Pressure = 12.37 psia)
MCU Fuel 1 - Horizontal Tank

Aneth, Utah 

TANKS 4.0.9d

Emissions Report - Detail Format 

Liquid Contents of Storage Tank

Daily Liquid Surf. 

Temperature (deg F)

Liquid 

Bulk 

Temp Vapor Pressure (psia)

Vapor

Mol. 

Liquid

Mass 

Vapor

Mass Mol. Basis for Vapor Pressure

Mixture/Component Month Avg. Min. Max. (deg F) Avg. Min. Max. Weight. Fract. Fract. Weight Calculations

Gasoline (RVP 10) All 55.06 48.57 61.56 52.95 4.7080 4.1342 5.3442 66.0000 92.00 Option 4: RVP=10, ASTM Slope=3
MCU Fuel 1 - Horizontal Tank

Aneth, Utah 

TANKS 4.0.9d

Emissions Report - Detail Format 

Detail Calculations (AP-42)

Annual Emission Calcaulations 

Standing Losses (lb): 1,742.0456

 Vapor Space Volume (cu ft): 845.2285

 Vapor Density (lb/cu ft): 0.0563

 Vapor Space Expansion Factor: 0.2006

 Vented Vapor Saturation Factor: 0.5005

Tank Vapor Space Volume: 

 Vapor Space Volume (cu ft): 845.2285

 Tank Diameter (ft): 8.0000

 Effective Diameter (ft): 16.4026

 Vapor Space Outage (ft): 4.0000

 Tank Shell Length (ft): 26.4000

Vapor Density 

 Vapor Density (lb/cu ft): 0.0563

 Vapor Molecular Weight (lb/lb-mole): 66.0000

 Vapor Pressure at Daily Average Liquid 

 Surface Temperature (psia): 4.7080

 Daily Avg. Liquid Surface Temp. (deg. R): 514.7342

 Daily Average Ambient Temp. (deg. F): 52.9333

 Ideal Gas Constant R 

 (psia cuft / (lb-mol-deg R)): 10.731

 Liquid Bulk Temperature (deg. R): 512.6233

 Tank Paint Solar Absorptance (Shell): 0.1700

 Daily Total Solar Insulation 

 Factor (Btu/sqft day): 1,578.3125

Vapor Space Expansion Factor 

 Vapor Space Expansion Factor: 0.2006

 Daily Vapor Temperature Range (deg. R): 25.9688

 Daily Vapor Pressure Range (psia): 1.2099

 Breather Vent Press. Setting Range(psia): 0.0600

 Vapor Pressure at Daily Average Liquid 

 Surface Temperature (psia): 4.7080

 Vapor Pressure at Daily Minimum Liquid 

 Surface Temperature (psia): 4.1342

 Vapor Pressure at Daily Maximum Liquid 

 Surface Temperature (psia): 5.3442

 Daily Avg. Liquid Surface Temp. (deg R): 514.7342

 Daily Min. Liquid Surface Temp. (deg R): 508.2420

 Daily Max. Liquid Surface Temp. (deg R): 521.2264

 Daily Ambient Temp. Range (deg. R): 25.6333

Vented Vapor Saturation Factor 

 Vented Vapor Saturation Factor: 0.5005

 Vapor Pressure at Daily Average Liquid: 

 Surface Temperature (psia): 4.7080

 Vapor Space Outage (ft): 4.0000

Working Losses (lb): 748.7276

 Vapor Molecular Weight (lb/lb-mole): 66.0000

 Vapor Pressure at Daily Average Liquid 

 Surface Temperature (psia): 4.7080

 Annual Net Throughput (gal/yr.): 101,202.0000

 Annual Turnovers: 10.1895

 Turnover Factor: 1.0000

 Tank Diameter (ft): 8.0000

 Working Loss Product Factor: 1.0000

Total Losses (lb): 2,490.7732
Emissions Report for: Annual 

MCU Fuel 1 - Horizontal Tank

Aneth, Utah 

TANKS 4.0.9d

Emissions Report - Detail Format 

Individual Tank Emission Totals

Losses(lbs)

Components Working Loss Breathing Loss Total Emissions

Gasoline (RVP 10) 748.73 1,742.05 2,490.77
TANKS 4.0.9d

Emissions Report - Detail Format 

Tank Indentification and Physical Characteristics

Identification

 User Identification: MCU Fuel 1

 City: Aneth

 State: Utah

 Company: Resolute

 Type of Tank: Horizontal Tank

 Description: 1,000 gal Fuel Tank at MCU Central Facility

Tank Dimensions

 Shell Length (ft): 26.40

 Diameter (ft): 8.00

 Volume (gallons): 9,932.00

 Turnovers: 12.08

 Net Throughput(gal/yr): 121,443.00

 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): -0.03

 Pressure Settings (psig) 0.03

Meterological Data used in Emissions Calculations: Grand Junction, Colorado (Avg Atmospheric Pressure = 12.37 psia)
MCU Fuel 1 - Horizontal Tank

Aneth, Utah 

TANKS 4.0.9d

Emissions Report - Detail Format 

Liquid Contents of Storage Tank

Daily Liquid Surf. 

Temperature (deg F)

Liquid 

Bulk 

Temp Vapor Pressure (psia)

Vapor

Mol. 

Liquid

Mass 

Vapor

Mass Mol. Basis for Vapor Pressure

Mixture/Component Month Avg. Min. Max. (deg F) Avg. Min. Max. Weight. Fract. Fract. Weight Calculations

Gasoline (RVP 10) All 55.06 48.57 61.56 52.95 4.7080 4.1342 5.3442 66.0000 92.00 Option 4: RVP=10, ASTM Slope=3
MCU Fuel 1 - Horizontal Tank

Aneth, Utah 

TANKS 4.0.9d

Emissions Report - Detail Format 

Detail Calculations (AP-42)

Annual Emission Calcaulations 

Standing Losses (lb): 1,742.0456

 Vapor Space Volume (cu ft): 845.2285

 Vapor Density (lb/cu ft): 0.0563

 Vapor Space Expansion Factor: 0.2006

 Vented Vapor Saturation Factor: 0.5005

Tank Vapor Space Volume: 

 Vapor Space Volume (cu ft): 845.2285

 Tank Diameter (ft): 8.0000

 Effective Diameter (ft): 16.4026

 Vapor Space Outage (ft): 4.0000

 Tank Shell Length (ft): 26.4000

Vapor Density 

 Vapor Density (lb/cu ft): 0.0563

 Vapor Molecular Weight (lb/lb-mole): 66.0000

 Vapor Pressure at Daily Average Liquid 

 Surface Temperature (psia): 4.7080

 Daily Avg. Liquid Surface Temp. (deg. R): 514.7342

 Daily Average Ambient Temp. (deg. F): 52.9333

 Ideal Gas Constant R 

 (psia cuft / (lb-mol-deg R)): 10.731

 Liquid Bulk Temperature (deg. R): 512.6233

 Tank Paint Solar Absorptance (Shell): 0.1700

 Daily Total Solar Insulation 

 Factor (Btu/sqft day): 1,578.3125

Vapor Space Expansion Factor 

 Vapor Space Expansion Factor: 0.2006

 Daily Vapor Temperature Range (deg. R): 25.9688

 Daily Vapor Pressure Range (psia): 1.2099

 Breather Vent Press. Setting Range(psia): 0.0600

 Vapor Pressure at Daily Average Liquid 

 Surface Temperature (psia): 4.7080

 Vapor Pressure at Daily Minimum Liquid 

 Surface Temperature (psia): 4.1342

 Vapor Pressure at Daily Maximum Liquid 

 Surface Temperature (psia): 5.3442

 Daily Avg. Liquid Surface Temp. (deg R): 514.7342

 Daily Min. Liquid Surface Temp. (deg R): 508.2420

 Daily Max. Liquid Surface Temp. (deg R): 521.2264

 Daily Ambient Temp. Range (deg. R): 25.6333

Vented Vapor Saturation Factor 

 Vented Vapor Saturation Factor: 0.5005

 Vapor Pressure at Daily Average Liquid: 

 Surface Temperature (psia): 4.7080

 Vapor Space Outage (ft): 4.0000

Working Losses (lb): 898.4776

 Vapor Molecular Weight (lb/lb-mole): 66.0000

 Vapor Pressure at Daily Average Liquid 

 Surface Temperature (psia): 4.7080

 Annual Net Throughput (gal/yr.): 121,443.0000

 Annual Turnovers: 12.0822

 Turnover Factor: 1.0000

 Tank Diameter (ft): 8.0000

 Working Loss Product Factor: 1.0000

Total Losses (lb): 2,640.5232
Emissions Report for: Annual 

MCU Fuel 1 - Horizontal Tank

Aneth, Utah 

TANKS 4.0.9d

Emissions Report - Detail Format 

Individual Tank Emission Totals

Losses(lbs)

Components Working Loss Breathing Loss Total Emissions

Gasoline (RVP 10) 898.48 1,742.05 2,640.52
 Page: 1

GRI-GLYCalc VERSION 4.0 - AGGREGATE CALCULATIONS REPORT

Case Name: MCU_DEHY_2011

File Name: C:\Documents and Settings\dmallory\Desktop\MCU PSD\Nov 2012 Follow

Up\MCU_DEHY_2011_ACTUAL.ddf

 Date: November 29, 2012

 DESCRIPTION:

 Description: Existing Dehy at MCU Plant

 2011 Actual Emissions

 Annual Hours of Operation: 8760.0 hours/yr

 EMISSIONS REPORTS:

 -------------------------------------------------------------------

 CONTROLLED REGENERATOR EMISSIONS

 -------------------------------------------------------------------

 Component lbs/hr lbs/day tons/yr 

 ------------------------------- ----------- ----------- -----------

 Hydrogen Sulfide 0.0002 0.004 0.0008

 Methane 0.0011 0.027 0.0049

 Ethane 0.0084 0.202 0.0369

 Propane 0.0320 0.768 0.1402

 Isobutane 0.0093 0.224 0.0408

 n-Butane 0.0421 1.010 0.1843

 Isopentane 0.0134 0.321 0.0586

 n-Pentane 0.0210 0.504 0.0920

 Cyclopentane 0.0006 0.013 0.0025

 n-Hexane 0.0100 0.239 0.0437

 Cyclohexane 0.0213 0.512 0.0935

 Heptanes 0.0106 0.255 0.0465

 Methylcyclohexane 0.0194 0.466 0.0850

 Benzene 0.1153 2.768 0.5051

 Toluene 0.1257 3.016 0.5504

 Ethylbenzene 0.0201 0.481 0.0878

 Xylenes 0.0920 2.209 0.4031

 C8+ Heavies 0.0303 0.727 0.1328

 ------------------------------- ----------- ----------- -----------

 Total Emissions 0.5728 13.748 2.5090

 Total Hydrocarbon Emissions 0.5726 13.744 2.5082

 Total VOC Emissions 0.5631 13.514 2.4663

 Total HAP Emissions 0.3630 8.713 1.5901

 Total BTEX Emissions 0.3531 8.474 1.5464

 UNCONTROLLED REGENERATOR EMISSIONS

 -------------------------------------------------------------------

 Component lbs/hr lbs/day tons/yr 

 ------------------------------- ----------- ----------- -----------

 Hydrogen Sulfide 0.0036 0.087 0.0158

 Methane 0.0226 0.542 0.0989

 Ethane 0.1687 4.049 0.7390

 Propane 0.6401 15.361 2.8034

 Isobutane 0.1863 4.472 0.8161

 n-Butane 0.8417 20.200 3.6865

 Isopentane 0.2676 6.422 1.1720

 n-Pentane 0.4201 10.082 1.8399

 Cyclopentane 0.0112 0.269 0.0491
 Page: 2

 n-Hexane 0.1995 4.789 0.8740

 Cyclohexane 0.4270 10.247 1.8700

 Heptanes 0.2124 5.098 0.9304

 Methylcyclohexane 0.3882 9.318 1.7005

 Benzene 2.3063 55.352 10.1018

 Toluene 2.5135 60.323 11.0090

 Ethylbenzene 0.4011 9.625 1.7566

 Xylenes 1.8405 44.173 8.0615

 C8+ Heavies 0.6062 14.549 2.6551

 ------------------------------- ----------- ----------- -----------

 Total Emissions 11.4565 274.957 50.1796

 Total Hydrocarbon Emissions 11.4529 274.870 50.1638

 Total VOC Emissions 11.2616 270.279 49.3260

 Total HAP Emissions 7.2609 174.262 31.8028

 Total BTEX Emissions 7.0614 169.473 30.9289

 FLASH GAS EMISSIONS

 -------------------------------------------------------------------

 Component lbs/hr lbs/day tons/yr 

 ------------------------------- ----------- ----------- -----------

 Hydrogen Sulfide <0.0001 <0.001 <0.0001

 Methane 0.0092 0.221 0.0404

 Ethane 0.0158 0.378 0.0690

 Propane 0.0207 0.497 0.0907

 Isobutane 0.0034 0.081 0.0148

 n-Butane 0.0107 0.256 0.0467

 Isopentane 0.0026 0.062 0.0114

 n-Pentane 0.0031 0.074 0.0135

 Cyclopentane <0.0001 0.001 0.0001

 n-Hexane 0.0007 0.016 0.0030

 Cyclohexane 0.0004 0.009 0.0017

 Heptanes 0.0003 0.007 0.0013

 Methylcyclohexane 0.0002 0.006 0.0010

 Benzene 0.0002 0.005 0.0008

 Toluene 0.0001 0.003 0.0005

 Ethylbenzene <0.0001 <0.001 <0.0001

 Xylenes <0.0001 0.001 0.0001

 C8+ Heavies 0.0002 0.005 0.0009

 ------------------------------- ----------- ----------- -----------

 Total Emissions 0.0676 1.622 0.2959

 Total Hydrocarbon Emissions 0.0676 1.621 0.2959

 Total VOC Emissions 0.0426 1.022 0.1865

 Total HAP Emissions 0.0010 0.024 0.0045

 Total BTEX Emissions 0.0003 0.008 0.0015

 FLASH TANK OFF GAS

 -------------------------------------------------------------------

 Component lbs/hr lbs/day tons/yr 

 ------------------------------- ----------- ----------- -----------

 Hydrogen Sulfide 0.0002 0.004 0.0008

 Methane 0.1842 4.422 0.8070

 Ethane 0.3152 7.564 1.3804

 Propane 0.4143 9.942 1.8145

 Isobutane 0.0678 1.627 0.2969

 n-Butane 0.2133 5.120 0.9344

 Isopentane 0.0519 1.245 0.2272

 n-Pentane 0.0615 1.477 0.2696

 Cyclopentane 0.0004 0.010 0.0019
 Page: 3

 n-Hexane 0.0136 0.326 0.0596

 Cyclohexane 0.0076 0.183 0.0334

 Heptanes 0.0059 0.143 0.0261

 Methylcyclohexane 0.0047 0.112 0.0204

 Benzene 0.0038 0.092 0.0168

 Toluene 0.0023 0.054 0.0099

 Ethylbenzene 0.0002 0.004 0.0008

 Xylenes 0.0005 0.012 0.0023

 C8+ Heavies 0.0039 0.094 0.0171

 ------------------------------- ----------- ----------- -----------

 Total Emissions 1.3513 32.432 5.9189

 Total Hydrocarbon Emissions 1.3512 32.428 5.9181

 Total VOC Emissions 0.8518 20.442 3.7307

 Total HAP Emissions 0.0204 0.489 0.0893

 Total BTEX Emissions 0.0068 0.163 0.0297

 COMBINED REGENERATOR VENT/FLASH GAS EMISSIONS

 -------------------------------------------------------------------

 Component lbs/hr lbs/day tons/yr 

 ------------------------------- ----------- ----------- -----------

 Hydrogen Sulfide 0.0002 0.005 0.0008

 Methane 0.0103 0.248 0.0453

 Ethane 0.0242 0.581 0.1060

 Propane 0.0527 1.265 0.2309

 Isobutane 0.0127 0.305 0.0556

 n-Butane 0.0527 1.266 0.2310

 Isopentane 0.0160 0.383 0.0700

 n-Pentane 0.0241 0.578 0.1055

 Cyclopentane 0.0006 0.014 0.0025

 n-Hexane 0.0107 0.256 0.0467

 Cyclohexane 0.0217 0.521 0.0952

 Heptanes 0.0109 0.262 0.0478

 Methylcyclohexane 0.0196 0.471 0.0860

 Benzene 0.1155 2.772 0.5059

 Toluene 0.1258 3.019 0.5509

 Ethylbenzene 0.0201 0.481 0.0879

 Xylenes 0.0921 2.209 0.4032

 C8+ Heavies 0.0305 0.732 0.1336

 ------------------------------- ----------- ----------- -----------

 Total Emissions 0.6404 15.369 2.8049

 Total Hydrocarbon Emissions 0.6402 15.365 2.8041

 Total VOC Emissions 0.6057 14.536 2.6528

 Total HAP Emissions 0.3641 8.738 1.5946

 Total BTEX Emissions 0.3534 8.482 1.5479

 COMBINED REGENERATOR VENT/FLASH GAS EMISSION CONTROL REPORT:

 -------------------------------------------------------------------

 Component Uncontrolled Controlled % Reduction

 tons/yr tons/yr 

 ------------------------------- ------------ ------------ ------------

 Hydrogen Sulfide 0.0166 0.0008 95.00

 Methane 0.9059 0.0453 95.00

 Ethane 2.1194 0.1060 95.00

 Propane 4.6179 0.2309 95.00

 Isobutane 1.1130 0.0556 95.00

 n-Butane 4.6209 0.2310 95.00
 Page: 4

 Isopentane 1.3992 0.0700 95.00

 n-Pentane 2.1095 0.1055 95.00

 Cyclopentane 0.0510 0.0025 95.00

 n-Hexane 0.9335 0.0467 95.00

 Cyclohexane 1.9035 0.0952 95.00

 Heptanes 0.9565 0.0478 95.00

 Methylcyclohexane 1.7209 0.0860 95.00

 Benzene 10.1186 0.5059 95.00

 Toluene 11.0189 0.5509 95.00

 Ethylbenzene 1.7574 0.0879 95.00

 Xylenes 8.0638 0.4032 95.00

 C8+ Heavies 2.6722 0.1336 95.00

 ------------------------------- ------------ ------------ ------------

 Total Emissions 56.0985 2.8049 95.00

 Total Hydrocarbon Emissions 56.0819 2.8041 95.00

 Total VOC Emissions 53.0566 2.6528 95.00

 Total HAP Emissions 31.8921 1.5946 95.00

 Total BTEX Emissions 30.9586 1.5479 95.00

 EQUIPMENT REPORTS:

 -------------------------------------------------------------------

 COMBUSTION DEVICE

 -------------------------------------------------------------------

 Ambient Temperature: 70.00 deg. F

 Excess Oxygen: 0.00 %

 Combustion Efficiency: 95.00 %

 Supplemental Fuel Requirement: 5.62e-002 MM BTU/hr

 Component Emitted Destroyed 

 ------------------------------- ----------- -----------

 Hydrogen Sulfide 5.00% 95.00%

 Methane 5.00% 95.00%

 Ethane 5.00% 95.00%

 Propane 5.00% 95.00%

 Isobutane 5.00% 95.00%

 n-Butane 5.00% 95.00%

 Isopentane 5.00% 95.00%

 n-Pentane 5.00% 95.00%

 Cyclopentane 5.00% 95.00%

 n-Hexane 5.00% 95.00%

 Cyclohexane 5.00% 95.00%

 Heptanes 5.00% 95.00%

 Methylcyclohexane 5.00% 95.00%

 Benzene 5.00% 95.00%

 Toluene 5.00% 95.00%

 Ethylbenzene 5.00% 95.00%

 Xylenes 5.00% 95.00%

 C8+ Heavies 5.00% 95.00%

 ABSORBER

 -------------------------------------------------------------------

 Specified Absorber Stages: 2.00

 Calculated Dry Gas Dew Point: 7.33 lbs. H2O/MMSCF

 Temperature: 100.0 deg. F
 Page: 5

 Pressure: 250.0 psig

 Dry Gas Flow Rate: 4.3600 MMSCF/day

 Glycol Losses with Dry Gas: 0.0321 lb/hr

 Wet Gas Water Content: Saturated

 Calculated Wet Gas Water Content: 188.20 lbs. H2O/MMSCF

 Specified Lean Glycol Recirc. Ratio: 3.00 gal/lb H2O

 Remaining Absorbed 

 Component in Dry Gas in Glycol 

 ------------------------------- ----------- -----------

 Water 3.87% 96.13%

 Carbon Dioxide 99.83% 0.17%

 Hydrogen Sulfide 98.85% 1.15%

 Nitrogen 99.99% 0.01%

 Methane 99.99% 0.01%

 Ethane 99.96% 0.04%

 Propane 99.91% 0.09%

 Isobutane 99.86% 0.14%

 n-Butane 99.81% 0.19%

 Isopentane 99.78% 0.22%

 n-Pentane 99.72% 0.28%

 Cyclopentane 98.85% 1.15%

 n-Hexane 99.49% 0.51%

 Cyclohexane 97.89% 2.11%

 Heptanes 98.95% 1.05%

 Methylcyclohexane 97.32% 2.68%

 Benzene 83.10% 16.90%

 Toluene 74.19% 25.81%

 Ethylbenzene 60.71% 39.29%

 Xylenes 48.49% 51.51%

 C8+ Heavies 92.55% 7.45%

 FLASH TANK

 -------------------------------------------------------------------

 Flash Control: Combustion device

 Flash Control Efficiency: 95.00 %

 Flash Temperature: 60.0 deg. F

 Flash Pressure: 80.0 psig

 Left in Removed in

 Component Glycol Flash Gas 

 ------------------------------- ----------- -----------

 Water 100.00% 0.00%

 Carbon Dioxide 71.08% 28.92%

 Hydrogen Sulfide 95.28% 4.72%

 Nitrogen 10.41% 89.59%

 Methane 10.91% 89.09%

 Ethane 34.87% 65.13%

 Propane 60.71% 39.29%

 Isobutane 73.32% 26.68%

 n-Butane 79.78% 20.22%

 Isopentane 83.84% 16.16%

 n-Pentane 87.28% 12.72%

 Cyclopentane 96.31% 3.69%

 n-Hexane 93.65% 6.35%

 Cyclohexane 98.30% 1.70%

 Heptanes 97.29% 2.71%

 Methylcyclohexane 98.86% 1.14%

 Benzene 99.84% 0.16%

 Toluene 99.92% 0.08%
 Page: 6

 Ethylbenzene 99.96% 0.04%

 Xylenes 99.98% 0.02%

 C8+ Heavies 99.44% 0.56%

 REGENERATOR

 -------------------------------------------------------------------

 No Stripping Gas used in regenerator.

 Remaining Distilled 

 Component in Glycol Overhead 

 ------------------------------- ----------- -----------

 Water 29.60% 70.40%

 Carbon Dioxide 0.00% 100.00%

 Hydrogen Sulfide 0.00% 100.00%

 Nitrogen 0.00% 100.00%

 Methane 0.00% 100.00%

 Ethane 0.00% 100.00%

 Propane 0.00% 100.00%

 Isobutane 0.00% 100.00%

 n-Butane 0.00% 100.00%

 Isopentane 0.60% 99.40%

 n-Pentane 0.57% 99.43%

 Cyclopentane 0.52% 99.48%

 n-Hexane 0.53% 99.47%

 Cyclohexane 3.26% 96.74%

 Heptanes 0.51% 99.49%

 Methylcyclohexane 4.05% 95.95%

 Benzene 5.01% 94.99%

 Toluene 7.91% 92.09%

 Ethylbenzene 10.40% 89.60%

 Xylenes 12.90% 87.10%

 C8+ Heavies 12.06% 87.94%

 STREAM REPORTS:

 -------------------------------------------------------------------

 WET GAS STREAM

 -------------------------------------------------------------

 Temperature: 100.00 deg. F

 Pressure: 264.70 psia

 Flow Rate: 1.83e+005 scfh

 Component Conc. Loading 

 (vol%) (lb/hr) 

 ------------------------------- --------- ---------

 Water 3.96e-001 3.44e+001

 Carbon Dioxide 5.95e+001 1.26e+004

 Hydrogen Sulfide 2.00e-003 3.28e-001

 Nitrogen 1.28e+000 1.73e+002

 Methane 2.21e+001 1.71e+003

 Ethane 7.62e+000 1.10e+003

 Propane 5.28e+000 1.12e+003

 Isobutane 6.32e-001 1.77e+002

 n-Butane 1.95e+000 5.44e+002

 Isopentane 4.14e-001 1.44e+002
 Page: 7

 n-Pentane 4.93e-001 1.71e+002

 Cyclopentane 3.00e-003 1.01e+000

 n-Hexane 1.01e-001 4.19e+001

 Cyclohexane 5.10e-002 2.06e+001

 Heptanes 4.30e-002 2.07e+001

 Methylcyclohexane 3.10e-002 1.46e+001

 Benzene 3.64e-002 1.37e+001

 Toluene 2.20e-002 9.75e+000

 Ethylbenzene 2.00e-003 1.02e+000

 Xylenes 6.99e-003 3.57e+000

 C8+ Heavies 9.99e-003 8.19e+000

 ------------------------------- --------- ---------

 Total Components 100.00 1.79e+004

 DRY GAS STREAM

 -------------------------------------------------------------

 Temperature: 100.00 deg. F

 Pressure: 264.70 psia

 Flow Rate: 1.82e+005 scfh

 Component Conc. Loading 

 (vol%) (lb/hr) 

 ------------------------------- --------- ---------

 Water 1.54e-002 1.33e+000

 Carbon Dioxide 5.97e+001 1.26e+004

 Hydrogen Sulfide 1.99e-003 3.24e-001

 Nitrogen 1.29e+000 1.73e+002

 Methane 2.22e+001 1.71e+003

 Ethane 7.66e+000 1.10e+003

 Propane 5.31e+000 1.12e+003

 Isobutane 6.35e-001 1.77e+002

 n-Butane 1.95e+000 5.43e+002

 Isopentane 4.15e-001 1.43e+002

 n-Pentane 4.94e-001 1.71e+002

 Cyclopentane 2.98e-003 1.00e+000

 n-Hexane 1.01e-001 4.16e+001

 Cyclohexane 5.01e-002 2.02e+001

 Heptanes 4.27e-002 2.05e+001

 Methylcyclohexane 3.03e-002 1.42e+001

 Benzene 3.04e-002 1.14e+001

 Toluene 1.64e-002 7.23e+000

 Ethylbenzene 1.22e-003 6.20e-001

 Xylenes 3.41e-003 1.73e+000

 C8+ Heavies 9.30e-003 7.58e+000

 ------------------------------- --------- ---------

 Total Components 100.00 1.79e+004

 LEAN GLYCOL STREAM

 -------------------------------------------------------------

 Temperature: 100.00 deg. F

 Flow Rate: 1.64e+000 gpm

 Component Conc. Loading 

 (wt%) (lb/hr) 

 ------------------------------- --------- ---------

 TEG 9.84e+001 9.11e+002

 Water 1.50e+000 1.39e+001

 Carbon Dioxide 2.25e-010 2.09e-009

 Hydrogen Sulfide 4.09e-014 3.78e-013

 Nitrogen 2.30e-013 2.13e-012
 Page: 8

 Methane 7.50e-019 6.95e-018

 Ethane 2.47e-008 2.28e-007

 Propane 4.64e-009 4.29e-008

 Isobutane 8.24e-010 7.63e-009

 n-Butane 2.83e-009 2.62e-008

 Isopentane 1.73e-004 1.61e-003

 n-Pentane 2.62e-004 2.42e-003

 Cyclopentane 6.32e-006 5.85e-005

 n-Hexane 1.16e-004 1.07e-003

 Cyclohexane 1.55e-003 1.44e-002

 Heptanes 1.19e-004 1.10e-003

 Methylcyclohexane 1.77e-003 1.64e-002

 Benzene 1.31e-002 1.22e-001

 Toluene 2.33e-002 2.16e-001

 Ethylbenzene 5.03e-003 4.66e-002

 Xylenes 2.94e-002 2.73e-001

 C8+ Heavies 8.98e-003 8.31e-002

 ------------------------------- --------- ---------

 Total Components 100.00 9.26e+002

 RICH GLYCOL STREAM

 -------------------------------------------------------------

 Temperature: 100.00 deg. F

 Pressure: 264.70 psia

 Flow Rate: 1.78e+000 gpm

 NOTE: Stream has more than one phase.

 Component Conc. Loading 

 (wt%) (lb/hr) 

 ------------------------------- --------- ---------

 TEG 9.18e+001 9.11e+002

 Water 4.73e+000 4.69e+001

 Carbon Dioxide 2.10e+000 2.09e+001

 Hydrogen Sulfide 3.81e-004 3.78e-003

 Nitrogen 2.12e-003 2.11e-002

 Methane 2.08e-002 2.07e-001

 Ethane 4.88e-002 4.84e-001

 Propane 1.06e-001 1.05e+000

 Isobutane 2.56e-002 2.54e-001

 n-Butane 1.06e-001 1.05e+000

 Isopentane 3.24e-002 3.21e-001

 n-Pentane 4.88e-002 4.84e-001

 Cyclopentane 1.18e-003 1.17e-002

 n-Hexane 2.16e-002 2.14e-001

 Cyclohexane 4.52e-002 4.49e-001

 Heptanes 2.21e-002 2.19e-001

 Methylcyclohexane 4.12e-002 4.09e-001

 Benzene 2.45e-001 2.43e+000

 Toluene 2.75e-001 2.73e+000

 Ethylbenzene 4.51e-002 4.48e-001

 Xylenes 2.13e-001 2.11e+000

 C8+ Heavies 6.99e-002 6.93e-001

 ------------------------------- --------- ---------

 Total Components 100.00 9.92e+002

 FLASH TANK OFF GAS STREAM

 -------------------------------------------------------------

 Temperature: 60.00 deg. F
 Page: 9

 Pressure: 94.70 psia

 Flow Rate: 6.68e+001 scfh

 Component Conc. Loading 

 (vol%) (lb/hr) 

 ------------------------------- --------- ---------

 Water 3.01e-002 9.56e-004

 Carbon Dioxide 7.79e+001 6.03e+000

 Hydrogen Sulfide 2.97e-003 1.78e-004

 Nitrogen 3.83e-001 1.89e-002

 Methane 6.52e+000 1.84e-001

 Ethane 5.95e+000 3.15e-001

 Propane 5.34e+000 4.14e-001

 Isobutane 6.62e-001 6.78e-002

 n-Butane 2.08e+000 2.13e-001

 Isopentane 4.08e-001 5.19e-002

 n-Pentane 4.85e-001 6.15e-002

 Cyclopentane 3.50e-003 4.32e-004

 n-Hexane 8.96e-002 1.36e-002

 Cyclohexane 5.15e-002 7.63e-003

 Heptanes 3.37e-002 5.95e-003

 Methylcyclohexane 2.70e-002 4.66e-003

 Benzene 2.79e-002 3.83e-003

 Toluene 1.39e-002 2.26e-003

 Ethylbenzene 9.57e-004 1.79e-004

 Xylenes 2.78e-003 5.20e-004

 C8+ Heavies 1.30e-002 3.90e-003

 ------------------------------- --------- ---------

 Total Components 100.00 7.40e+000

 FLASH TANK GLYCOL STREAM

 -------------------------------------------------------------

 Temperature: 60.00 deg. F

 Flow Rate: 1.77e+000 gpm

 Component Conc. Loading 

 (wt%) (lb/hr) 

 ------------------------------- --------- ---------

 TEG 9.25e+001 9.11e+002

 Water 4.77e+000 4.69e+001

 Carbon Dioxide 1.51e+000 1.48e+001

 Hydrogen Sulfide 3.66e-004 3.61e-003

 Nitrogen 2.23e-004 2.19e-003

 Methane 2.29e-003 2.26e-002

 Ethane 1.71e-002 1.69e-001

 Propane 6.50e-002 6.40e-001

 Isobutane 1.89e-002 1.86e-001

 n-Butane 8.55e-002 8.42e-001

 Isopentane 2.73e-002 2.69e-001

 n-Pentane 4.29e-002 4.23e-001

 Cyclopentane 1.14e-003 1.13e-002

 n-Hexane 2.04e-002 2.01e-001

 Cyclohexane 4.48e-002 4.41e-001

 Heptanes 2.17e-002 2.14e-001

 Methylcyclohexane 4.11e-002 4.05e-001

 Benzene 2.47e-001 2.43e+000

 Toluene 2.77e-001 2.73e+000

 Ethylbenzene 4.55e-002 4.48e-001

 Xylenes 2.15e-001 2.11e+000

 C8+ Heavies 7.00e-002 6.89e-001
 Page: 10

 ------------------------------- --------- ---------

 Total Components 100.00 9.85e+002

 FLASH GAS EMISSIONS

 -------------------------------------------------------------

 Flow Rate: 1.32e+002 scfh

 Control Method: Combustion Device

 Control Efficiency: 95.00 

 Component Conc. Loading 

 (vol%) (lb/hr) 

 ------------------------------- --------- ---------

 Water 3.51e+001 2.20e+000

 Carbon Dioxide 6.41e+001 9.83e+000

 Hydrogen Sulfide 7.52e-005 8.92e-006

 Nitrogen 1.94e-001 1.89e-002

 Methane 1.65e-001 9.21e-003

 Ethane 1.50e-001 1.58e-002

 Propane 1.35e-001 2.07e-002

 Isobutane 1.67e-002 3.39e-003

 n-Butane 5.27e-002 1.07e-002

 Isopentane 1.03e-002 2.59e-003

 n-Pentane 1.22e-002 3.08e-003

 Cyclopentane 8.84e-005 2.16e-005

 n-Hexane 2.27e-003 6.80e-004

 Cyclohexane 1.30e-003 3.82e-004

 Heptanes 8.52e-004 2.97e-004

 Methylcyclohexane 6.82e-004 2.33e-004

 Benzene 7.04e-004 1.92e-004

 Toluene 3.52e-004 1.13e-004

 Ethylbenzene 2.42e-005 8.95e-006

 Xylenes 7.03e-005 2.60e-005

 C8+ Heavies 3.29e-004 1.95e-004

 ------------------------------- --------- ---------

 Total Components 100.00 1.21e+001

 REGENERATOR OVERHEADS STREAM

 -------------------------------------------------------------

 Temperature: 212.00 deg. F

 Pressure: 14.70 psia

 Flow Rate: 8.79e+002 scfh

 Component Conc. Loading 

 (vol%) (lb/hr) 

 ------------------------------- --------- ---------

 Water 7.92e+001 3.30e+001

 Carbon Dioxide 1.46e+001 1.48e+001

 Hydrogen Sulfide 4.57e-003 3.61e-003

 Nitrogen 3.38e-003 2.19e-003

 Methane 6.08e-002 2.26e-002

 Ethane 2.42e-001 1.69e-001

 Propane 6.27e-001 6.40e-001

 Isobutane 1.38e-001 1.86e-001

 n-Butane 6.25e-001 8.42e-001

 Isopentane 1.60e-001 2.68e-001

 n-Pentane 2.51e-001 4.20e-001

 Cyclopentane 6.90e-003 1.12e-002

 n-Hexane 1.00e-001 2.00e-001

 Cyclohexane 2.19e-001 4.27e-001

 Heptanes 9.15e-002 2.12e-001
 Page: 11

 Methylcyclohexane 1.71e-001 3.88e-001

 Benzene 1.28e+000 2.31e+000

 Toluene 1.18e+000 2.51e+000

 Ethylbenzene 1.63e-001 4.01e-001

 Xylenes 7.49e-001 1.84e+000

 C8+ Heavies 1.54e-001 6.06e-001

 ------------------------------- --------- ---------

 Total Components 100.00 5.93e+001

 COMBUSTION DEVICE OFF GAS STREAM

 -------------------------------------------------------------

 Temperature: 1000.00 deg. F

 Pressure: 14.70 psia

 Flow Rate: 2.73e+000 scfh

 Component Conc. Loading 

 (vol%) (lb/hr) 

 ------------------------------- --------- ---------

 Hydrogen Sulfide 7.35e-002 1.80e-004

 Methane 9.78e-001 1.13e-003

 Ethane 3.90e+000 8.44e-003

 Propane 1.01e+001 3.20e-002

 Isobutane 2.23e+000 9.32e-003

 n-Butane 1.01e+001 4.21e-002

 Isopentane 2.58e+000 1.34e-002

 n-Pentane 4.04e+000 2.10e-002

 Cyclopentane 1.11e-001 5.60e-004

 n-Hexane 1.61e+000 9.98e-003

 Cyclohexane 3.52e+000 2.13e-002

 Heptanes 1.47e+000 1.06e-002

 Methylcyclohexane 2.75e+000 1.94e-002

 Benzene 2.05e+001 1.15e-001

 Toluene 1.89e+001 1.26e-001

 Ethylbenzene 2.62e+000 2.01e-002

 Xylenes 1.20e+001 9.20e-002

 C8+ Heavies 2.47e+000 3.03e-002

 ------------------------------- --------- ---------

 Total Components 100.00 5.73e-001
 Page: 1

GRI-GLYCalc VERSION 4.0 - SUMMARY OF INPUT VALUES

Case Name: MCU_DEHY_2011

File Name: C:\Documents and Settings\dmallory\Desktop\MCU PSD\Nov 2012 Follow

Up\MCU_DEHY_2011_ACTUAL.ddf

 Date: November 29, 2012

 DESCRIPTION:

 -------------------------------------------------------------------

 Description: Existing Dehy at MCU Plant

 2011 Actual Emissions

 Annual Hours of Operation: 8760.0 hours/yr

 WET GAS:

 -------------------------------------------------------------------

 Temperature: 100.00 deg. F

 Pressure: 250.00 psig

 Wet Gas Water Content: Saturated

 Component Conc. 

 (vol %) 

 ------------------------------- -----------

 Carbon Dioxide 59.5700

 Hydrogen Sulfide 0.0020

 Nitrogen 1.2860

 Methane 22.1210

 Ethane 7.6310

 Propane 5.2880

 Isobutane 0.6330

 n-Butane 1.9480

 Isopentane 0.4140

 n-Pentane 0.4930

 Cyclopentane 0.0030

 n-Hexane 0.1010

 Cyclohexane 0.0510

 Heptanes 0.0430

 Methylcyclohexane 0.0310

 Benzene 0.0364

 Toluene 0.0220

 Ethylbenzene 0.0020

 Xylenes 0.0070

 C8+ Heavies 0.0100

 DRY GAS:

 -------------------------------------------------------------------

 Flow Rate: 4.4 MMSCF/day

 Absorber Stages: 2.0

 LEAN GLYCOL:

 -------------------------------------------------------------------

 Glycol Type: TEG

 Water Content: 1.5 wt% H2O

 Recirculation Ratio: 3.0 gal/lb H2O

 PUMP:

 -------------------------------------------------------------------
 Page: 2

 Glycol Pump Type: Electric/Pneumatic

 FLASH TANK:

 -------------------------------------------------------------------

 Flash Control: Combustion device

 Flash Control Efficiency: 95.00 %

 Temperature: 60.0 deg. F

 Pressure: 80.0 psig

 REGENERATOR OVERHEADS CONTROL DEVICE:

 -------------------------------------------------------------------

 Control Device: Combustion Device

 Destruction Efficiency: 95.0 %

 Excess Oxygen: 0.0 %

 Ambient Air Temperature: 70.0 deg. F
 Page: 1

GRI-GLYCalc VERSION 4.0 - EMISSIONS SUMMARY

Case Name: MCU_DEHY_PTE

File Name: C:\Documents and Settings\dmallory\Desktop\MCU PSD\Nov 2012 Follow

Up\MCU_DEHY_PTE_4_PSD.ddf

 Date: November 29, 2012

 CONTROLLED REGENERATOR EMISSIONS

 -------------------------------------------------------------------

 Component lbs/hr lbs/day tons/yr 

 ------------------------------- ----------- ----------- -----------

 Hydrogen Sulfide 0.0005 0.012 0.0022

 Methane 0.0031 0.075 0.0136

 Ethane 0.0232 0.557 0.1017

 Propane 0.0881 2.113 0.3857

 Isobutane 0.0256 0.615 0.1123

 n-Butane 0.1158 2.779 0.5072

 Isopentane 0.0368 0.884 0.1612

 n-Pentane 0.0578 1.387 0.2531

 Cyclopentane 0.0015 0.037 0.0068

 n-Hexane 0.0275 0.659 0.1202

 Cyclohexane 0.0587 1.410 0.2573

 Heptanes 0.0292 0.701 0.1280

 Methylcyclohexane 0.0534 1.282 0.2339

 Benzene 0.3173 7.615 1.3898

 Toluene 0.3458 8.299 1.5146

 Ethylbenzene 0.0552 1.324 0.2417

 Xylenes 0.2532 6.078 1.1092

 C8+ Heavies 0.0834 2.002 0.3653

 ------------------------------- ----------- ----------- -----------

 Total Emissions 1.5762 37.829 6.9037

 Total Hydrocarbon Emissions 1.5757 37.817 6.9016

 Total VOC Emissions 1.5494 37.185 6.7863

 Total HAP Emissions 0.9990 23.975 4.3755

 Total BTEX Emissions 0.9715 23.317 4.2553

 UNCONTROLLED REGENERATOR EMISSIONS

 -------------------------------------------------------------------

 Component lbs/hr lbs/day tons/yr 

 ------------------------------- ----------- ----------- -----------

 Hydrogen Sulfide 0.0099 0.238 0.0435

 Methane 0.0621 1.491 0.2720

 Ethane 0.4642 11.141 2.0333

 Propane 1.7611 42.267 7.7138

 Isobutane 0.5127 12.304 2.2455

 n-Butane 2.3159 55.581 10.1435

 Isopentane 0.7363 17.670 3.2248

 n-Pentane 1.1559 27.741 5.0627

 Cyclopentane 0.0308 0.740 0.1351

 n-Hexane 0.5490 13.177 2.4047

 Cyclohexane 1.1748 28.194 5.1454

 Heptanes 0.5845 14.028 2.5601

 Methylcyclohexane 1.0682 25.638 4.6789

 Benzene 6.3461 152.306 27.7959

 Toluene 6.9161 165.986 30.2924

 Ethylbenzene 1.1036 26.486 4.8337

 Xylenes 5.0648 121.555 22.1837

 C8+ Heavies 1.6679 40.030 7.3056

 ------------------------------- ----------- ----------- -----------
 Page: 2

 Total Emissions 31.5239 756.573 138.0746

 Total Hydrocarbon Emissions 31.5140 756.335 138.0311

 Total VOC Emissions 30.9876 743.703 135.7258

 Total HAP Emissions 19.9796 479.509 87.5105

 Total BTEX Emissions 19.4305 466.333 85.1057

 FLASH GAS EMISSIONS

 -------------------------------------------------------------------

 Component lbs/hr lbs/day tons/yr 

 ------------------------------- ----------- ----------- -----------

 Hydrogen Sulfide <0.0001 0.001 0.0001

 Methane 0.0253 0.608 0.1110

 Ethane 0.0434 1.041 0.1899

 Propane 0.0570 1.368 0.2496

 Isobutane 0.0093 0.224 0.0408

 n-Butane 0.0293 0.704 0.1285

 Isopentane 0.0071 0.171 0.0313

 n-Pentane 0.0085 0.203 0.0371

 Cyclopentane 0.0001 0.001 0.0003

 n-Hexane 0.0019 0.045 0.0082

 Cyclohexane 0.0010 0.025 0.0046

 Heptanes 0.0008 0.020 0.0036

 Methylcyclohexane 0.0006 0.015 0.0028

 Benzene 0.0005 0.013 0.0023

 Toluene 0.0003 0.007 0.0014

 Ethylbenzene <0.0001 0.001 0.0001

 Xylenes 0.0001 0.002 0.0003

 C8+ Heavies 0.0005 0.013 0.0024

 ------------------------------- ----------- ----------- -----------

 Total Emissions 0.1859 4.462 0.8143

 Total Hydrocarbon Emissions 0.1859 4.461 0.8142

 Total VOC Emissions 0.1172 2.812 0.5133

 Total HAP Emissions 0.0028 0.067 0.0123

 Total BTEX Emissions 0.0009 0.022 0.0041

 FLASH TANK OFF GAS

 -------------------------------------------------------------------

 Component lbs/hr lbs/day tons/yr 

 ------------------------------- ----------- ----------- -----------

 Hydrogen Sulfide 0.0005 0.012 0.0022

 Methane 0.5070 12.167 2.2205

 Ethane 0.8672 20.812 3.7982

 Propane 1.1399 27.357 4.9927

 Isobutane 0.1865 4.476 0.8169

 n-Butane 0.5870 14.088 2.5710

 Isopentane 0.1427 3.426 0.6252

 n-Pentane 0.1694 4.064 0.7418

 Cyclopentane 0.0012 0.029 0.0052

 n-Hexane 0.0374 0.898 0.1639

 Cyclohexane 0.0210 0.504 0.0920

 Heptanes 0.0164 0.393 0.0717

 Methylcyclohexane 0.0128 0.308 0.0562

 Benzene 0.0105 0.253 0.0462

 Toluene 0.0062 0.149 0.0272

 Ethylbenzene 0.0005 0.012 0.0022

 Xylenes 0.0014 0.034 0.0063

 C8+ Heavies 0.0107 0.258 0.0470

 ------------------------------- ----------- ----------- -----------
 Page: 3

 Total Emissions 3.7183 89.239 16.2861

 Total Hydrocarbon Emissions 3.7178 89.227 16.2840

 Total VOC Emissions 2.3437 56.248 10.2653

 Total HAP Emissions 0.0561 1.346 0.2457

 Total BTEX Emissions 0.0187 0.448 0.0818

 COMBINED REGENERATOR VENT/FLASH GAS EMISSIONS

 -------------------------------------------------------------------

 Component lbs/hr lbs/day tons/yr 

 ------------------------------- ----------- ----------- -----------

 Hydrogen Sulfide 0.0005 0.012 0.0023

 Methane 0.0285 0.683 0.1246

 Ethane 0.0666 1.598 0.2916

 Propane 0.1451 3.481 0.6353

 Isobutane 0.0350 0.839 0.1531

 n-Butane 0.1451 3.483 0.6357

 Isopentane 0.0439 1.055 0.1925

 n-Pentane 0.0663 1.590 0.2902

 Cyclopentane 0.0016 0.038 0.0070

 n-Hexane 0.0293 0.704 0.1284

 Cyclohexane 0.0598 1.435 0.2619

 Heptanes 0.0300 0.721 0.1316

 Methylcyclohexane 0.0541 1.297 0.2368

 Benzene 0.3178 7.628 1.3921

 Toluene 0.3461 8.307 1.5160

 Ethylbenzene 0.0552 1.325 0.2418

 Xylenes 0.2533 6.079 1.1095

 C8+ Heavies 0.0839 2.014 0.3676

 ------------------------------- ----------- ----------- -----------

 Total Emissions 1.7621 42.291 7.7180

 Total Hydrocarbon Emissions 1.7616 42.278 7.7158

 Total VOC Emissions 1.6666 39.998 7.2996

 Total HAP Emissions 1.0018 24.043 4.3878

 Total BTEX Emissions 0.9725 23.339 4.2594
 Page: 1

GRI-GLYCalc VERSION 4.0 - SUMMARY OF INPUT VALUES

Case Name: MCU_DEHY_PTE

File Name: C:\Documents and Settings\dmallory\Desktop\MCU PSD\Nov 2012 Follow

Up\MCU_DEHY_PTE_4_PSD.ddf

 Date: November 29, 2012

 DESCRIPTION:

 -------------------------------------------------------------------

 Description: Existing Dehy at MCU Plant

 Potential to Emit for PSD Permit Draft

 November 2012

 Annual Hours of Operation: 8760.0 hours/yr

 WET GAS:

 -------------------------------------------------------------------

 Temperature: 100.00 deg. F

 Pressure: 250.00 psig

 Wet Gas Water Content: Saturated

 Component Conc. 

 (vol %) 

 ------------------------------- -----------

 Carbon Dioxide 59.5700

 Hydrogen Sulfide 0.0020

 Nitrogen 1.2860

 Methane 22.1210

 Ethane 7.6310

 Propane 5.2880

 Isobutane 0.6330

 n-Butane 1.9480

 Isopentane 0.4140

 n-Pentane 0.4930

 Cyclopentane 0.0030

 n-Hexane 0.1010

 Cyclohexane 0.0510

 Heptanes 0.0430

 Methylcyclohexane 0.0310

 Benzene 0.0364

 Toluene 0.0220

 Ethylbenzene 0.0020

 Xylenes 0.0070

 C8+ Heavies 0.0100

 DRY GAS:

 -------------------------------------------------------------------

 Flow Rate: 12.0 MMSCF/day

 Absorber Stages: 2.0

 LEAN GLYCOL:

 -------------------------------------------------------------------

 Glycol Type: TEG

 Water Content: 1.5 wt% H2O

 Recirculation Ratio: 3.0 gal/lb H2O

 PUMP:
 Page: 2

 -------------------------------------------------------------------

 Glycol Pump Type: Electric/Pneumatic

 FLASH TANK:

 -------------------------------------------------------------------

 Flash Control: Combustion device

 Flash Control Efficiency: 95.00 %

 Temperature: 60.0 deg. F

 Pressure: 80.0 psig

 REGENERATOR OVERHEADS CONTROL DEVICE:

 -------------------------------------------------------------------

 Control Device: Combustion Device

 Destruction Efficiency: 95.0 %

 Excess Oxygen: 0.0 %

 Ambient Air Temperature: 70.0 deg. F