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Next Generation OBIGGS : Developments at Phyre Technologies

Next Generation OBIGGS : Developments at Phyre Technologies . Santosh Y. Limaye Phyre Technologies, Inc. November 2, 2005 Atlantic City, NJ Presented at International Aircraft Systems Fire Protection Working Group Meeting. The Concept.

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Next Generation OBIGGS : Developments at Phyre Technologies

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  1. Next Generation OBIGGS: Developments at Phyre Technologies Santosh Y. Limaye Phyre Technologies, Inc. November 2, 2005 Atlantic City, NJ Presented at International Aircraft Systems Fire Protection Working Group Meeting

  2. The Concept • Treat the ullage from the fuel tank to create inert gas • Inexpensive catalytic system • Avoid the use of bleed air This concept resulted from liquid fuel de-oxygenation system development

  3. Filamentous Amorphous Condensation 14 12 10 pyrolytic deposits thermal-oxidative deposits 8 Combustor 6 4 900 1100 700 300 500 800 1000 600 400 Fuel Temperature, F 2 600 200 300 500 Fuel Temperature, C 400 0 JP-8 JP-8+100 JP-8+225 JP-900 Endo JP Fuel Flow Endothermic fuels JP-8 JP-8+100 JP-8+225 JP-900 High Heat Sink Fuels Benefits • Increase Thrust-to-weight • enables higher T41 • Reduce take-off gross weight • reduce fuel recirculation & ram air HX wt • Improve SFC • enables higher T3 and P3 • Reduce component operating temp. • higher heat sink capability High Heat Sink Fuels:Enable Advanced Propulsion >1300 F Deposition is The Significant Challenge for High Heat Sink Fuels Heat sink relative to JP-8 900 F 550 F 425 F 325 F Near term Mid - Term

  4. Inert Gas Fuel Gas Contactor Contaminated Fuel Fuel Gas Separator De-Oxygenated Fuel Inert Gas + O2 + Fuel Vapor Gas Treatment System Pump Oxygen free gas For Recycling Quick Review of De-Oxygenation System Removing dissolved oxygen in fuel prevents premature oxidation; a primary cause of coking. Dissolved oxygen = cholesterol

  5. Mass Transfer Issue Mass Transfer Region O2 Concentration Gradient Diesel Droplet in N2 Gas N2 Bubble in Diesel

  6. 60 50 40 Concentration (ppm) 30 O2 = 5 ppm 20 2 10 O 0 0 0.5 1 1.5 2 2.5 3 3.5 4 Fuel Flow (lpm) Does it work? - - YES! Fuel O2 = 57.9 ± 5.4 ppm N2 flow: 2.5 Liter/Min; lpm

  7. Results from Testing at AFRL Run75 Run79/81 Baseline JP-8 PADS Deox JP-8 (Catalyst) Run80 Run76 PADS Deox JP-8 (Nitrogen) JP-8+100 PADS DeOx JP-8 (LN2)

  8. OBIGGS

  9. OBIGGS Considerations 15 10 Dilution with Air Hydrocarbon Vapor Volume Fraction (%) Inert Air Purge 5 Flammability Region Critical Dilution with Air 5 10 15 20 Oxygen Volume Fraction (%)

  10. Catalytic Inerting System (CIS): Next Generation OBIGGS Concept Make up air to consume hydrocarbon vapor and pressure equalization Catalytic Gas Treatment System <10% oxygen + Fuel vapor + CO2 H2O + N2 21% oxygen + Fuel vapor + N2 safety device Air + Fuel Vapor Pump Water trap Fuel PATENT PENDING

  11. CIS System Description Low Temp. air to air Heat Exchangers Inlet Oxygen Sample Port Reverse Flow Valve Heat Exchanger & Heaters Reverse Flow Valve Blower Catalyst Bed, 5” Dia x 4.5”length Inlet Size: 12”x12”x 40” Capacity: 150 CFM # of passes to 10% O2 : 3 Outlet Control Unit Water Drain Support Systems Power Automatic Moisture Drain Valves Oxygen Sensors Optional, High Removal Rate, Vapor Fuel Control

  12. CIS Catalytic Chemistry • Saturated vapor phase of fuel vapor : C9H20 (Nonane) • As per DOT/FAA/AR-04/8 report (page 12), the precise composition is C9.05H18.01 • Vapor pressure of Nonane is estimated to be 8000 ppmv at 70F • Stoichiometric Reaction of 8000 ppmv Nonane will consume 112,000 ppmv (or 11.2%) oxygen to provide 70,000 (7%) and 40,000 (4%) ppmv of CO2 and H2O .008 @ 70F Stoichiometric Reaction C9H20 + 14O2 + 52.67 N2 9 CO2 + 10 H2O + 52.67 N2

  13. Oxygen Removal Rate • If H2O is removed from the product, additional fresh air is needed to compensate the gas pressure in the reactant. • The corrected O2 column shows new concentration based on fresh addition of air to replace water molecules. • Three passes will ensure reduction of O2 below 10%.

  14. CSR Model: Oxygen Depletion RateFor 450 Cu. Ft. Ullage

  15. Experimental limitations: • Very small ullage volume • Limited flow rate control • Objective was proof of concept to validate theoretical calculations • Limitations on catalyst volume (smallest 1.2 cc) • Delayed response due to long oxygen sensor lines Experimental Schematic Pump Moisture trap Catalyst Downstream Temp. CDT Post Catalyst O2 Conc. Ullage O2 Conc. Catalyst Controller for heater Oxygen Sensor* Heater Ullage Volume VU Flow Rate FR Catalyst Temp. CT Fuel Volume VF Flow Meter Pressure gage Fuel Tank

  16. Initial Results – Experiment #1

  17. Conclusion Benefits • No need for bleed air, eliminate ozone destruction device • Low temperature process • Only power necessary: blower operation • Smaller foot-print, lighter weight, lower cost • Closed loop system • Ability to reduce oxygen level as well as fuel vapor level Other Concerns Addressed • Use of fuel vapor phase means no sulfur contamination, no corrosion • Instead of purging the fuel vapor, it is consumed in the process, hence no VOC emissions from the tank • Ability to precisely control gas partial pressures Next Steps • Prototype Development • Testing Phase • Strategic Partnership Development

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