HYDROGEN R&D AT INEEL - Stanford UniversityJoseph C. Perkowski, Ph.D. 208-526-5232 April 27, 2004...
Transcript of HYDROGEN R&D AT INEEL - Stanford UniversityJoseph C. Perkowski, Ph.D. 208-526-5232 April 27, 2004...
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Idaho National Engineering and Environmental Laboratory
HYDROGEN R&D AT INEELOverview
Joseph C. Perkowski, Ph.D.
208-526-5232
April 27, 2004
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Long-Term Vision: “The Hydrogen Model Community”• A “Hydrogen City” or “Hydrogen Corridor” • INEEL, SE Idaho or other venue• Emphasis on engineering validation• Variations
– Treasure Valley Clean Air Non-Attainment Support– Hydrogen Yellow Bus for Greater Yellowstone Ecosystem– GHG-free Southern Idaho Corridor
Electrolysis
PrimaryEnergy Sources
Hydrogen Production
Transport Storage Distribution Use
Photo Conversion
or Compression
Electrolysis
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INEEL Hydrogen Initiative Objectives• Achieve a leading position in RD&D of key hydrogen technologies.
– Focus areas:1. Hydrogen production - nuclear energy,2. Hydrogen production - fossil and/or renewable energy,3. Hydrogen infrastructure - bulk hydrogen handling, vehicle fueling
infrastructure, vehicle testing, fuel cell fabrication/testing.• Gain increased stature as a multipurpose laboratory.• Contribute to the nation’s energy security and an improved
environment.
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Nuclear Hydrogen Production Development Plan
Research and DevelopmentEngineering Demonstration50 MW TC5 MW HTE
Lab Scale
Integrated Lab Scale
Pilot Scale5 MW TC0.5 MW HTE
Demonstration
• Thermochemical (TC)• High Temperature Electrolysis (HTE)• Heat Exchangers and BOP• Membrane and Other
2004 2006 2010 2017
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Hydrogen Production Using Nuclear Energy,INEEL Role
• Program integration and management (w/ Sandia)• Integrated laboratory scale tests• Pilot scale tests • Engineering demonstration • Enabling technology research – kinetics/catalysis, materials,
separations, electrolysis
Thermochemical Cycle High Temperature Electrolysis
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Hydrogen Production Using Fossil or Renewable Energy, INEEL Role• Technology Development and Demonstration
– Reformer processes– Modeling – Gasification technology demonstration– Gas cleanup
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Hydrogen Infrastructure/Utilization,INEEL Role• Fueling infrastructure, vehicle testing
• Distributed hydrogen generation– Electrolysis, liquid fuel reforming/cleanup
• Bulk hydrogen separation, delivery, storage • Fuel cell fabrication/demonstrations
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Idaho National Engineering and Environmental Laboratory
Absorption of CO2 by Aqueous Diethanolamine Solutions in a Vortex Tube Gas-Liquid Contactor and Separator
Participants: INEEL: Daniel S. Wendt,
(208-526-3996, [email protected])Michael G. Mc Kellar(208-526-1346, [email protected])Anna K. PodgorneyDouglas E. StaceyTerry D. Turner
ConocoPhillips Canada:Kevin T. Raterman
May 6, 2003
Supported by U.S. DOE (DESupported by U.S. DOE (DE--AC07AC07--99ID13727)99ID13727)
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Project Objectives:
• Low capital cost due to compact, simple design• High CO2 capture efficiency
– high efficiency mass transfer– reduced solvent regeneration requirements
• Operationally flexible– turn-down & scale-up with parallel design– easily accommodates variable flow rates and gas
compositions – low maintenance/portable configuration
• Works equally well for physical / chemical absorbents
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Jet type absorbers highly efficientReactor Type kl a ( s-1 x 100)
Packed tower 7
Sieve plate 40
Venturi reactor 25
Bubble column 24
Impinging jet 122
(Herskowits et. al.)
High Shear Jet Absorber
• highly turbulent... large interfacialarea for mass transfer
• multiple jets… impingement zone creates secondary drop breakup / greater area for mass transfer
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High Efficiency Absorption…. acid gas separation
• Co-inject chemical or physical absorbent–– COCO22 + 2R+ 2R22NH NH ↔ RR22NCOONCOO-- + R+ R22NHNH22
++
–– RR22NCOONCOO-- + H+ H22O O ↔ RR22NH + HCONH + HCO33--
–– R designates R designates ––CC22HH44--OHOH• Mass transfer rate ~ f(interfacial area, film thickness)• Vortex tube
– high differential gas-liquid acceleration - small drops– high turbulence - small film thickness
• GOAL … achieve near equilibrium acid gas loading
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Vortex Tube with Liquid Separator
Lorey, et. al., 1998
Cool Gas Outlet8 atm2 °C
Gas Inlet12.6 atm9 °C
Hot Gas Outlet8.6 atm7 °C
Liquid Outlet
J-T Temperature = 5 °C
•Joule-Thomson expansion•near sonic to supersonic velocity
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Scaled Contactor Process-wellhead (~Mscfd) to full gas plant (~MMscfd)-distributed engine (~Mscfd) to centralized power plant (~MMscfd)
Flash
Feed CO2 MixCO2
CO2
StripperAbsorbent
Clean Gas
Parallel Vortex Contactors
(Heat Regeneration if needed)Simple Process Schematic
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Vortex Contactor
Separator TubeSeparator TubeNozzleNozzle
Boroscope / Throttle
Vortex ContactorVortex Contactor
Gas Exit
Liquid inlet
Gas InletLiquid Exit
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Contactor Prototype
60 SLPM @ 100 psia inlet
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Gas - Liquid Loading Tests
• Achieve >95% gas-liquid separation for stoichiometric loading of a 15% volume CO2mixture
• Design parameters– vortex inlet– tube design
• tapered & slotted• stepped with holes
– tube length
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Stepped tube design exceeds gas/liquid separation target
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Inlet Liquid Flow Rate (cm3/minute)
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Stepped tube design exceeds gas/liquid separation target
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CO2/DEA Baseline Test Apparatus
CO2supply
N2supply
Reg Reg
CO2 FlowController
N2 FlowController
P
T
T P
GasChromato-
graph
P
P
Flowmeter
Liquid
T
Exit HighFlow
Exit LowFlow
TescomCheck Valve
Tescom
Liquid Pump
LiquidCollect-
ionVessel
LiquidCoalescer
VacuumPump
Hood
Atmosphere
Atmosphere
Vortex Tube
Air InletPress.
Air InletTemp.
Hot AirOutletTemp.
Hot ExitPress.
LiquidOutletTemp
LiquidInlet
Press.
ExitPress.
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CO2/DEA Baseline Testing Operation
• Operating Parameters– 100-500 cm3/min liquid flow rate– 15-50 wt% liquid DEA composition– 80-200 psig inlet gas pressure– 5-15 mol% inlet gas CO2 composition– 25-75 slpm inlet gas flow rate (dependent variable)
• Solvent loading and CO2 capture efficiency unsatisfactory in baseline testing
• Diagnostic testing indicated increased residence time required –process modifications necessary
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Process Modifications
• Modifications to process hardware– increase gas-liquid contact time– capacity to adjust the gas-liquid contactor geometric configuration– maintain ability to control the inlet gas pressure and CO2 : DEA
feed stream mole ratio• Modifications to process operating parameters
– 75-350 cm3/min liquid flow rate– 30 wt% liquid DEA composition– 70 slpm inlet gas flow rate– 10 mol% inlet gas CO2 composition– 170-250 psig inlet gas pressure (dependent variable)
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Baseline and Modified Process Configurations
CO2supply
N2supply
Reg Reg
CO2 FlowController
N2 FlowController
P
T
T P
GasChromato-
graph
P
P
Flowmeter
LiquidSupply
T
Exit HighFlow
Exit LowFlow
Check Valve
Liquid Pump
LiquidCollect-
ionVessel
LiquidCoalescer
VacuumPump
Hood
Atmosphere
Atmosphere
Air InletPress.
Air InletTemp.
Hot AirOutletTemp.
Hot ExitPress.
LiquidOutletTemp
LiquidInlet
Press.
ExitPress.
Contactor
TescomBack Press.Regulator
TescomBack Press.Regulator
ModifiedContactor/Separator
CO2supply
N2supply
Reg Reg
CO2 FlowController
N2 FlowController
P
T
T P
GasChromato-
graph
P
P
Flowmeter
Liquid
T
Exit HighFlow
Exit LowFlow
TescomCheck Valve
Tescom
Liquid Pump
LiquidCollect-
ionVessel
LiquidCoalescer
VacuumPump
Hood
Atmosphere
Atmosphere
Vortex Tube
Air InletPress.
Air InletTemp.
Hot AirOutletTemp.
Hot ExitPress.
LiquidOutletTemp
LiquidInlet
Press.
ExitPress.
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Inlet gas pressure as a function of liquid flow rate
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No Nozzle Fouling Nozzle Fouling Present
Fouling is caused by deposits accumulating in the vortex tube nozzles
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CO2 capture efficiency as function of liquid flow rate
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CO
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Mo dified Config urat ion 1Mo dified Config urat ion 2
Mo dified Config urat ion 3Mo dified Config urat ion 4Mo dified Config urat ion 5
Mo dified Config urat ion 6Mo dified Config urat ion 7Mo dified Config urat ion 8
Mo dified Config urat ion 9Mo dified Config urat ion 10Mo dified Config urat ion 11Mo dified Config urat ion 12
30 wt% DEA, 10 % CO2, 90 p s ig15wt% DEA, 10 % CO2, 90 p s ig30 wt% DEA, 10 % CO2, MAX ps ig
50wt% DEA, 10% CO2, 10 0 ps ig
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CO2 capture efficiency as function of liquid flow rate (no fouling)
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Modified Configurat ion 1Modified Configurat ion 2Modified Configurat ion 9Modified Configurat ion 10Modified Configurat ion 11Modified Configurat ion 12
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CO2 capture efficiency as function of liquid flow rate (fouling present)
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Modified Co nfig uration 3Mod ified Co nfig uration 4Mod ified Co nfig uration 5Mod ified Co nfig uration 6Mod ified Co nfig uration 7Mod ified Co nfig uration 8
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Solvent loading as function of liquid flow rate
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e D
EA] Modifie d Configura t ion 1
Modif ie d Configura t ion 2
Modif ie d Configura t ion 3
Modif ie d Configura t ion 4
Modif ie d Configura t ion 5
Modif ie d Configura t ion 6
Modif ie d Configura t ion 7
Modif ie d Configura t ion 8
Modif ie d Configura t ion 9
Modif ie d Configura t ion 10
Modif ie d Configura t ion 11
Modif ie d Configura t ion 12
30wt % DEA, 10% CO2, 90 psig
15wt % DEA, 10% CO2, 90 psig
30wt % DEA, 10% CO2, MAX psig
50wt % DEA, 10% CO2, 100 psig
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Solvent loading as function of liquid flow rate (no fouling)
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Modified Co nfigurat ion 1Modified Co nfigurat ion 2Modified Co nfigurat ion 9Modified Co nfigurat ion 10Modified Co nfigurat ion 11Modified Co nfigurat ion 12
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Solvent loading as function of liquid flow rate (fouling present)
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Mo dified Config urat io n 3Mo dified Config urat io n 4Mo dified Config urat io n 5Mo dified Config urat io n 6Mo dified Config urat io n 7Mo dified Config urat io n 8
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Conclusions
• Gas/Liquid separation efficiencies in excess of 95%• Non-optimized vortex tube testing has resulted in
carbon dioxide capture efficiencies of up to 86%• Solvent loading as high as 0.49 moles CO2/mole
DEA
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Future Research/Applications
• Process hardware optimization• Scaled contactor and separator• Additional solvents• Additional CO2 applications• H2S
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References• Herskowits,D.; Herskowits,V.; Stephan, K .; Tamir. A.: Characterization of a two-phase
impinging jet absorber. II. Absorption with chemical reaction of CO2 in NaOH solutions. Chem. Eng. Science 45 (1990) 1281-1287
• Lorey, M., Steinle, J., Thomas, K. 1998. “Industrial Application of Vortex Tube Separation Technology Utilizing the Ranque-Hilsch Effect,” presented at the 1998 SPE European Petroleum Conference, The Hague, Netherlands, October 20-22.
• Chakma, A., Chornet, E., Overend, R. P., and Dawson, W. H., “Absorption of CO2 by Aqueous Diethanolamine (DEA) Solutions in a High Shear Jet Absorber”, The Canadian Journal of Chemical Engineering, Volume 68, August 1990.
• Lee, J. I., Otto, F. D., and Mather, A. E., “Solubility of Carbon Dioxide in Aqueous Diethanolamine Solutions at High Pressures”, Journal of Chemical and Engineering Data, Vol. 17, No. 4, 1972.