### 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 dra ft flare permit and we

need the following information available when we ar e 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 Hoven weep that Don Shepherd at the National Park Service asked for? T hanks 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 he lpful if you could get this info from Resolute and find out if t he company can provide
this info within the next month or so. Thanks.

1) Provide facility- wide actual emissions and PTE estimates for SO 2, CO, NOX, VOC , PM, PM10. and PM2.5. Section 3 of the 2008 PSD application provides emissions info for the Main Fl are only.

2) Provide actual emissions and PTE estimates for S O2, CO, NOX, VOC , PM, PM10. and PM2.5 for the following emission un its. 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/capaci ties 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 re garding the operational status of (i) the emissions units liste d in the current PSD permit and (ii) the other operations at the MCU fac ility.

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 1 997  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 th is information and clarify whether it is acceptable to use this descri ption 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: 415-947-3579Email: kelly.shaheerah@epa.gov Response 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.pdf1) Provide facility-wide actual emissions and PT E estimates for SO2, CO, NOX, VOC, PM, PM10 and PM2.5. Section 3 of the 2008 PSD application prov ides 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 atta ched 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 vol ume of gas combusted in the main flare in calendar year 2008, as well as the resulting em issions, exceeded the PTE values submitted in the 2008 application for NOx, CO and VOC.

The revised PTE estimates were derived using th e 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 wa s 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 volum e 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 deri ved 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 w eeks, 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 vo lume 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 fo r 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 un its are included in the attached spreadsheet.3) Verify the accuracy of the rat ed 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 indicate s 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 capaci ty (9,925 gal actual) and not 1,000 gallons.

The Glycol Heater (TEG Regenerator Ven t) has a maximum throughput of 12 MMCFD. However, the current facility configuration lim its 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 operation s at the MCU facility.

Equipment in current MCU Facility PS D 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/h r, 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 gasol ine storage tank that is used for refueling of vehicles.

5) EPA was provided the attached desc ription of the MCU facility by Mob il 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 attachme nt 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 pr ocesses listed in the response to question 4 and discussed in Paragr aph B, “Plant and Process Overview” of the attachment.2007‐2011ActualEmissionsandPTEEstimateVolume SO2NOx CO VOC PM Volume SO3NOx CO VOC PM SO2NOx CO VOC PM SO2NOx CO VOC PM SO2NOx CO VOC PMMMCF TPY TPY TPY TPY TPY MMCF TPY TPY TPY TPY TPY TPY TPY TPY TPY TPY TPY TPY TPY TPY TPY TPY TPY TPY TPY TPY2007640.416.8 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 0.0 0.0 0.0 0.0 2.0 0.0 16.8 13.1 69.9 88.9 1.420081,203.721.0 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 0.0 0.0 0.0 0.0 2.0 0.0 21.0 25.5 137.3 168.9 2.82009416.019.3 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 0.0 0.0 0.0 0.0 2.0 0.0 19.3 8.8 46.2 57.3 0.92010289.412.8 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 0.0 0.0 0.0 0.0 2.0 0.0 12.8 6.2 32.2 43.1 0.72011423.426.7 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 0.0 0.0 0.0 0.0 2.0 0.0 26.7 8.8 46.2 59.6 0.9PTE 1,324.076.5 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 0.0 0.0 0.0 0.0 2.0 0.0 76.5 31.1 168.0 197.8 3.4McElmoCreekUnitCentralCompressionandReinjectionFacilityRegenerator Heater emissions from natural gas combustion were calculated using emissions factors from AP-42, Chapter 1, Table 1.4-1 and Table 1.4-2. Because fuel gas to the reboiler heater is not metered, the reboiler heaterwas 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 4.0.9d, and losses from refueling of vehicles and spillage, which were estimated using AP42 Section 5.2 emissions factors. Because itemized fuel invoices for the MCU tank were unavailable, annual gasoline throughputwas estimated using vehicle miles travelled from the most current 6 month period available and theestimated fuel economy of fleet vehicles. Because annual mileage records for previous years were unavailable, 2011 actual emissions were used for prior year's actual emissions as well.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 PTEestimates were derived using the same calculation methods, heat content and H2S concentrationassumptions specified in the 2008 PSD application. While the calculation methods and gas composition assumptions from the 2008application remain valid, the PTE volume of gas combusted in the Main Flare was revised from1,070,366 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 flare volume experienced at the facility since the 2008 PSD application.The 2008 PTE flare volume was derived using the actual volume of gas combusted in the Main Flare during calendar year 2003. The2003 volume, which was at that time the maximum annual volume of gas combusted in the MainFlare, was adjusted upward by 20% and the resulting gas volume was applied to the maximum gas heat content and H2S concentration values to determine the PTE for SO2, VOC, CO, NOx and PM. The revised PTE flarevolume 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 on an annual basis and includes gas combusted in the Main Flareduring a complete emergency shut down 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 beflared and provided an actual 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 volumewas only adjusted upward by 10% for PTE determination.YearFacility TotalMain Flare actual emissions for 2007 through 2011 were estimated using the calculation methods and site specific monthly gas composition as specified in the Exxon Mobil MCU Clean Air Act Consent Decree (DOJ Case No. 90-5-2-1-2237, 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)Gasoline Storage Tank(10,000 gal)Calculation Notes:Regenerator Vent VOC emissions were estimated using GRI-GLYCalc Version 4.0. Actual emissions for 2010 and 2011 were estimatedusing actual annual gas throughput and site specific gas analysis and glycol circulation data.Actual dehydrator gas throughput for 2007 through 2009 was not measured, so actual emissions for these years was determined using a conservative estimate of gas throughput. PTE for the dehydrator was estimated assuming12 MMCFD gas throughput and using the actual site specific gas analysis and glycol circulation data. Dehydrator flash gas and regenerator emissions are controlled by the Main Flare and both the Actual and PTE scenariosassume 95% VOC destruction efficiency. Regerator Vent NOx, CO and SO2 values reflect emissions from the Main Flare as a resultof the dehydrator emissions being combusted.RevisedNovember2012McElmoCreekUnitMainFlareActualEmissions2007‐2011Date Volume Flared SO2 NOx CO VOC PM2007CalendarYearTotals(MMCFandTPY)Date Volume Flared SO2 NOx CO VOC PM2008CalendarYearTotals(MMCFandTPY)Date Volume Flared SO2 NOx CO VOC PM2009CalendarYearTotals(MMCFandTPY)Date Volume Flared SO2 NOx CO VOC PM2010CalendarYearTotals(MMCFandTPY)Date Volume Flared SO2 NOx CO VOC PM2011CalendarYearTotals(MMCFandTPY)MainFlarePTERevisionV‐FlareVolume(kscf/yr) GHVMWSO2MWVOCMFH2SWFVOCERVOCERSO2ERNOxERCOERPM1,324,040 682.4 64.0 37.3 0.0 0.145 188.4 76.5 30.7 167.2 3.4EFNOx0.068 lbs/mmbtuEFCO0.37 lbs/mmbtuEFPM0.00745 lbs/mmbtuInputValues(seeAppendixBof2008PSDApplication) EmissionsRates(TPY)1,204 163.925.1 136.521.0289 38.25.8 31.512.8416 52.38.3 45.4640 83.912.7 69.216.819.31.42.80.90.60.9423 54.98.4 45.426.7Source: 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 Burne r A nnual Fuel Fuel Htg Fuel No. Equipment Rating Op Time Type V alue Use (MMBtu/Hr) (hours) (Btu/scf) (MMSCF/Year)

Fuel Use (MMSCF/Year) = Burner Rating (MMBtu/Hr) * 10 6 Btu/MMBtu * Operating Hours * 1 scf/1,020 Btu * 1 MMBtu/10 6 Btu

Emission Factors

Reference Burner No. Rating SO 2 NOx CO VOC PM 1
(MMBtu/Hr) (Lbs/10 6 scf) (Lbs/10 6 scf) (Lbs/10 6 scf) (Lbs/10 6 scf) (Lbs/10 6 scf)
Regenerator 0.750 0.6 100.0 84.0 5.5 7.6

A P-42 A P-42 A P-42 A P-42 A P-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 i s used used to estimate PM10, PM2.5 and PM1

Reference
No. SO 2 NOx CO VOC PM 1

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 GasFacility 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 Operation8,760Source with vapors sent to theCombustion ChamberNoteVaporVolume(scf/hr)VaporHeatingValue(btu/scf)H2SContent(%)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 1,267443.2 0.00 0.00 0.01 0.01 0.05 0.00 0.00Regenerator Vent 1,2879248.0 0.00 0.01 0.06 0.08 0.35 0.01 0.03Supplemental Fuel 1,255 1,020.0 0.000.00 0.02 0.02 0.09 0.00 0.00Total1,001 0.02 0.09 0.11 0.49 0.01 0.03NOTES: 1 - Flare NOx and CO emissions based on continuous operation, using emission factors from AP42, Chapter 13-52 - 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 ReportsDehydrator Control Flare Emission Analysis WorksheetLesair Environmental, Inc.www.lesair.comFacility 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 Operation8,760Source with vapors sent to theCombustion ChamberNoteVaporVolume(scf/hr)VaporHeatingValue(btu/scf)H2SContent(%)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 1,267443.4 0.00 0.00 0.01 0.01 0.05 0.00 0.00Regenerator Vent 1,2879273.3 0.01 0.02 0.07 0.09 0.39 0.01 0.03Supplemental Fuel 1,255 1,020.0 0.000.00 0.02 0.02 0.09 0.00 0.00Total1,001 0.02 0.10 0.12 0.53 0.01 0.03NOTES: 1 - Flare NOx and CO emissions based on continuous operation, using emission factors from AP42, Chapter 13-52 - 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 ReportsDehydrator Control Flare Emission Analysis WorksheetLesair Environmental, Inc.www.lesair.comAP-42 Section 5.2 Transportation And Marketing Of Petroleum LiquidsRefueling Losses= 11 lbs/10^3 Gal. Emissions Factor from AP42 Table 5.2-7Load Volume = 333 Gal/PD4 lbs/Day1335.9 lbs/YrSpillage Losses= 1 lbs/10^3 Gal. Emissions Factor from AP42 Table 5.2-7Load Volume = 333 Gal/PD0 lbs/Day85.0 lbs/YrTotal Refueling Losses 1420.9 lbs/YrEPA Tanks 4.0.9d Emissions Report for MCU Fuel Tank Working and Breathing Losses: AnnualMCU Fuel 1 - Horizontal TankAneth, UtahComponents Working Loss Breathing Loss Total EmissionsGasoline (RVP 10) 898.48 1,742.05 2,640.524,061 lbs/yr2.0 TPYMCUBulkGasolineTankEstimatedAnnualFuelThroughputTotal Units Total Miles Miles/Unit MCU Units MCU MilesAvg MPG1MCU GallonsAug-11 102 146,999 1,441 73 105,205 14 7,515Sep-11 103 161,294 1,566 73 114,315 14 8,165Oct-11 105 169,049 1,610 73 117,529 14 8,395Nov-11 105 167,565 1,596 73 116,498 14 8,321Dec-11 97 160,605 1,656 73 120,868 14 8,633Jan-12 93 170,714 1,836 73 134,001 14 9,57250,601MCU Avg Monthly Fuel Use 8,434 galMCU Annualized Fuel Use for PTE 121,443 galAvg 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 averagemiles 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 was thendivided 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 (RefuelingLosses + Working and Standing Losses)AP-42 Section 5.2 Transportation And Marketing Of Petroleum LiquidsRefueling Losses= 11 lbs/10^3 Gal. Emissions Factor from AP42 Table 5.2-7Load Volume = 333 Gal/PD4 lbs/Day1335.9 lbs/YrSpillage Losses= 1 lbs/10^3 Gal. Emissions Factor from AP42 Table 5.2-7Load Volume = 333 Gal/PD0 lbs/Day85.0 lbs/YrTotal Refueling Losses 1420.9 lbs/YrEPA Tanks 4.0.9d Emissions Report for MCU Fuel Tank Working and Breathing Losses: AnnualMCU Fuel 1 - Horizontal TankAneth, UtahComponents Working Loss Breathing Loss Total EmissionsGasoline (RVP 10) 748.73 1,742.05 2,490.773,912 lbs/yr2.0 TPYMCUBulkGasolineTankEstimatedAnnualFuelThroughputTotal Units Total Miles Miles/Unit MCU Units MCU MilesAvg MPG1MCU GallonsAug-11 102 146,999 1,441 73 105,205 14 7,515Sep-11 103 161,294 1,566 73 114,315 14 8,165Oct-11 105 169,049 1,610 73 117,529 14 8,395Nov-11 105 167,565 1,596 73 116,498 14 8,321Dec-11 97 160,605 1,656 73 120,868 14 8,633Jan-12 93 170,714 1,836 73 134,001 14 9,57250,601MCU Avg Monthly Fuel Use 8,434 galMCU Annualized Fuel Use for PTE 121,443 galAvg 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 averagemiles 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 was thendivided 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 (RefuelingLosses + Working and Standing Losses)MCUBulkGasolineTankEstimatedAnnualFuelThroughputTotalUnits TotalMiles Miles/Unit MCUUnits MCUMiles AvgMPG MCUGallonsAug‐11 102 146,999 1,441 73 105,205 14 7,515Sep‐11 103 161,294 1,566 73 114,315 14 8,165Oct‐11 105 169,049 1,610 73 117,529 14 8,395Nov‐11 105 167,565 1,596 73 116,498 14 8,321Dec‐11 97 160,605 1,656 73 120,868 14 8,633Jan‐12 93 170,714 1,836 73 134,001 14 9,57250,601MCUAvgMonthlyFuelUse 8,434 galMCUAnnualizedFuelUsefor2011Emissions 101,202 galMCUAnnualizedFuelUseforPTE 121,443 galAvgMPGistheEPA"City"mileageratingforthe2010FordF‐1504X4,whichisthestdfleetvehicleusedbyRNRCEstimatedfuelusefortheMCUgasolinestoragetankwasdeterminedusingthemostrecent6monthsofactualvehiclemileagethatwereavailable.Theaveragemilespervehiclewasmultipliedbythenumberofunitsassignedtothefacilitytoestimatethetotalmilesattributabletothefacility.Thetotalnumberofmileswasthendividedbytheestimatedaveragefueleconomyofthefleettoestimatethegallonsoffuelused.Thefuelgallonsusedwasincreasedby20%forPTEestimation.TANKS 4.0.9d Emissions Report - Detail Format
Tank Indentification an d Physical Characteristics

Identification User Identification: MCU Fuel 1 City: A neth State: Utah Compan y : 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 Throu g hput (g al/ y r ) : 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=3MCU Fuel 1 - Horizontal Tank Aneth, Utah TANKS 4.0.9d Emissions Report - Detail Format Detail Calculations (AP-42)

A nnual 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 ( de g . 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 Dail y 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): 2,490.7732Emissions 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 2,490.77TANKS 4.0.9d Emissions Report - Detail Format
Tank Indentification an d Physical Characteristics

Identification User Identification: MCU Fuel 1 City: A neth State: Utah Compan y : 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 Throu g hput (g al/ y r ) : 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=3MCU Fuel 1 - Horizontal Tank Aneth, Utah TANKS 4.0.9d Emissions Report - Detail Format Detail Calculations (AP-42)

A nnual 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 ( de g . 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 Dail y 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): 2,640.5232Emissions 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 2,640.52Page: 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 0.0491Page: 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 0.0019Page: 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 95.00Page: 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. FPage: 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+002Page: 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-012Page: 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. FPage: 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-001Page: 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-001Page: 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-001Page: 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. FPage: 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 4.2594Page: 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