1. FLASH EMISSIONS JIM COOPER, CHESAPEAKE ENERGY CORPORATION

2. OPERATING EQUIPMENT 2

3. FLASH GAS  Regulated Volatile Organic Compounds (C3+)  Flash gas from tanks include methane, ethane, and propane and higher components  Causes of Flash Gas › Results from high pressure to low pressure drop › Phase change from liquid to gas. Light ends volatilize with change in pressure or temperature  Primary source of VOC flash loss › Atmospheric tanks receiving liquids from oil separator 3

4. WORKING AND BREATHING LOSSES  Working Losses › Increase in evaporation due to filling the tank  Breathing Losses › Normal evaporation of liquid in a tank, volume increases with temperature increases 4

5. TANK EMISSIONS  For a typical tank that receives condensate or oil from a separator, emissions will include working, breathing, and flash losses. 5

6. TANK EMISSIONS – CALCULATION METHODS  Direct Measurement  E&P Tanks  Process Simulator Software  Laboratory Gas-Oil-Ratio (GOR)  Vasquez-Beggs Equation (VBE)  Tanks 4.09d 6

7. METHODOLOGY - OPTIONS  Direct Measurement › Expensive sampling, relatively accurate › Use appropriate methods and procedures for measurement and sampling › Includes flash, working and breathing 7

8. METHODOLOGY - OPTIONS  E&P Tanks › Site Specific (preferred) or Geographical Database  E&P Tanks Site Specific › Separator oil composition, Temperature, Pressure, API gravity, RVP 8

9. METHODOLOGY - OPTIONS  Process Simulator Software › PROMAX, WinSim, HYSIM, HYSIS › Reservoir analysis or pressurized liquid sample, extended analysis, RVP, API gravity › Must use AP-42 or Tanks 4.09d for working and breathing losses › Good option for sizing of equipment and permitting under different operating parameters 9

10. METHODOLOGY - OPTIONS  Tanks 4.09d › Working and breathing only  Gas-Oil-Ratio (GOR) - Pressurized Liquid Sample › Direct lab analysis of the flash gas in the oil / condensate sample › Sample from the last pressure vessel before the tanks › GOR, RVP, API gravity, separator temp and pressure 10

11. METHODOLOGY - OPTIONS  Vasquez-Beggs Equation (VBE) › Requires API gravity, separator temperature and pressure, and gas specific gravity. 11

12. EMISSION DETERMINATION  Identify representative oil or condensate sample › Use facility specific or representative field sample  Estimate maximum and actual production rates  Determine operating parameters for well and processing equipment  Use appropriate methodology for estimating emissions 12

13. FLASH RATE EXAMPLES FOR HEATER TREATER TO TANKS Operating pressures and temperatures GPU (F)70 PL (psig)250350 HT (psig)3045 HT (F)80120 LPT (psig)NA PL PressureHT Op PressureHT TempFlash Factor 25030806.97 2503012011.08 25045809.57 2504512015.56 35030807.73 3503012011.17 350458010.96 3504512016.31 13

14. FLASH RATE EXAMPLES FOR LOW PRESSURE TOWER TO TANKS GPU (F)70 PL (psig)250350 HT (psig)3045 HT (F)80120 LPT (psig)5 PL PressureHT Op PressureHT TempFlash Factor 25030801.55 250301202.48 25045801.49 250451202.44 35030801.74 350301202.51 35045801.73 350451202.56 14

15. HEATER TREATER  Designed to operate at specific flows, pressures, and temperatures  Allows flash gas to be captured prior to atmospheric storage tanks  Designed to operate at specific flows, pressures and temperatures 15

16. REDUCTION OPTIONS  Low pressure tower  Flash gas compression 16

17. LOW PRESSURE TOWER SYSTEM (LPT)  Also called vapor recovery tower (VRT)  Low pressure separator for liquid production sites  Puts rich gas vapors back in the pipeline  Can vent to flash gas compressor or flare Condensate/Oil In Flash Gas Out Condensate/Oil Out – Gravity Flow to Tanks Liquid Seal 17

18. LPT – Low Pressure Tower 30” diameter x 30’ tall Cost: $8K - $10K LPT – Low Pressure Tower 30” diameter x 30’ tall Cost: $8K - $10K 18

19. TANKS  Potentially vents VOCs to the atmosphere from Enardo valves and thief hatches if uncontrolled 19

20. 4” Vent Line to Flare 20

21. FLARES OR COMBUSTORS  Sizing › Designed for specific Btu loads / volumes › Must be sized to handle max load 21

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23. THE END 23