© IMM, March 2009
SUSTAINABLE ENERGY TECHNOLOGY - ETHANOL STEAM
REFORMING AS HYDROGEN SOURCE FOR FUEL CELLS
CPAC SATELLITE WORKSHOP 2009Micro-Reactors and Micro-Analytical Workshop
(with an emphasis on Bio Systems)
March 23-25, 2009Rome, Italy
Jochen Schuerer1 , Email: [email protected]
Volker Hessel1, 2
Gunther Kolb1
1Institut für Mikrotechnik Mainz GmbH (IMM), Germany
2Eindhoven University of Technology, Netherlands
© IMM, March 2009
IMM - Centre of Excellence in Microtechnology,Microfluidics & Micro Process Engineering
We are...
...a non-profit company owned by the federal state of Rheinland-Pfalz
...some 160 employees with mainly academic background
...an application oriented R&D institute
Main Fields of R&D work: Focus on Chemical Process Technology andMicrofluidics,Micro Precision Engineering, Thin Film Technology
Mixing and Fine Chemistry Department:Emulsions/Dispersions, Particles/Supramol. Assemblies, Fine & Bulk Chemistry
Energy Technology and Catalysis Department:Development of Complete Micro-structured Fuel Processors (Reactor Design &Construction, Development of Catalyst Coatings, Catalyst / Reactor / System Testing)Liquid Hydrogen Technology
© IMM, March 2009
Chemical Process Engineering (MUF)
Bio-Micro Fluidics
OUR CORE COMPETENCIES
Fuel Processing (EUK)
3D –Microstructuring Technologies
© IMM, March 2009
OVERVIEW
1. Micro-reaction technology and micro process engineering as anoption for process intensification and sustainabilityEuropean roadmap for process intensificationNovell process windowsScale out and scale up, from laboratory to pilot and production scaleFabrication techniques
2. Micro-reactor technologies for decentralized energy generationApplication of Micro-technology in Fuel Cells / Fuel Processors
3. Sustainable energy technology – ethanol steam reformingwith micro-reactorsBio-ethanol Steam-reformingExperimental characterization
March 2009
European Roadmap on Process Intensification, Creative Energies, Energy Transition, 2008
DEFINITIONS ON PROCESS IMPROVEMENT
Aim
Focus
Interdis-ciplinarity
Process optimization Process Systems Process intensificationEngineering
Performance improvement Multi-scale integration Development of new conceptsof existing concepts of existing/new concepts of process steps & equipment
Model, numerical method Model, software Experiment, phenomenon, interphase
Weak Modest StrongApplied mathematics Applied mathematics & Chemistry & catalysis, applied
informatics, chemistry physics, mechanical engineering,materials science, electronics, etc.
March 2009
Chip microflow devices (microreactor)Microstructured reactor
Foams Monoliths
Mini-packed bed reactors
Tube / Capillary reactors
• Fast mass transfer• Efficient heat management• Fast residence time• Regular flow patterns• Safe operation in explosive regimes• Small hold-up, …
Hessel, Hardt, Löwe, Chemical Micro Process Engineering -Fundamentals, Modelling and Reactions, Wiley-VCH, Weinheim 2004.Pennemann, Watts, Hessel et al., Org. Proc. Res. Dev 8. (2004) 422.Jähnisch, Hessel, Löwe, Baerns, Angew. Chem. Int. Ed. 43 (2004) 406.Hessel et al., Curr. Org. Chem. 2005, 9, 765.Jensen, Chem. Eng. Sci. 2001, 56, 293.Haswell, Watts, Green Chemistry 2003, 5, 240.Fletcher, Haswell, Watts et al., Tetrahedron 2002, 58, 4735.Gavriilidis et al., Trans. IChemE. 2002, 80/A, 3.Watts, QSAR Combinatorial Science 24 (2005) 701-711Geyer, Seeberger et al., Chem. European J. 12 (2006) 8434..Kolb, Hessel, Chem. Eng. J. 98 (2004) 1.Kiwi-Minsker, Renken, Catalysis Today 110 (2005) 2.Hessel, Löwe, Müller, Kolb, Chemical Micro Process Engineering -Processing and Plants, Wiley-VCH, Weinheim 2005.
Microreaction technologyMicro process engineering
FROM STRUCTURED MEDIA VIA STRUCTURED FLUIDS TO PROCESS INTENSIFICATION
March 2009
Catalysts & Microfluidics
Test devices
Scale-out devices
Systems
Processes & Plants
Laboratory scaleIn
dust
rial u
p to
Wor
ld s
cale
Pilot scaleGas-liquidFalling-film technology
Fuel Processing
Bulk Chemicals
Micro Process Engineering, Handbook in 3 Volumes, Wiley-VCH, Weinheim, March 2009
Novel Process WindowsUpfront cost and LCA analysis
MICRO PROCESS ENGINEERING
March 2009
27 INDUSTRIAL PILOT AND PRODUCTION CASES IN FINE AND BULK CHEMSTRY
Hessel, V., Löb, P., Löwe, H.; "Industrial Microreactor Process Development up to Production", in: "Micro-reactors for Organic Synthesis and Catalysis". ed.: Wirth, T., Wiley-VCH, Weinheim (2008).
Polycondensation (Japanese company)Friedel-Crafts alkylation (Japanese company)H2O2 based oxidation to 2-methyl-1,4-naphthoquinone (Japanese company)Direct fluorination of ethyl 3-oxobutanoate (Asahi Glass)Propene oxide formation (Degussa / Uhde)Vinyl acetate synthesis (Uhde)Lithiation of aromatic compounds (Brystol-Meyers-Squibb)Production of polymer intermediates (DSM Fine Chemicals GmbH)Production of diazo pigments (Clariant)Nitroglycerine production (Xi’an Company)Fine-chemical production (not disclosed)Grignard–based enolate production (Merck)
Hydrogen peroxide synthesis (UOP, FMC)Organolithium exchange reaction (Lonza)Chlorination (Lonza)Dehydrogenation (Lonza)Polyacrylate formation (Siemens-Axiva)Alkylation reactions based on butyl lithium (Lonza)DAST Fluorination (Bayer-Schering Pharma)Steroid Ozonolysis (Bayer-Schering Pharma)Plasma reaction (Degussa)Gas-liquid oxidation (Degussa)PMMA manufacture (Idemitsu Kosan)Grignard exchange reaction (Japanese Company)Halogen-Lithium exchange (Japanese Company)Swern-Moffat oxidation (Ube Industries)Yellow nano pigments (Fuji)
IMM Technology
March 2009
HYPOTHETICAL LIQUID-PHASE REACTION AT THE EDGE TO LARGE-SCALE PRODUCTION
0.2 4
2 0
2
4
6
8
10
12
14
16
18
20
100 120 140 160 180 200 220 240 260
Reaction temperature [°C]
Num
ber o
f rea
ctor
s
k=0.01 s-1
100°C
k=0.1 s-1
162°C k=1 s-1
249°C
k=0.05 s -1
141°C
250°C and 70 – 150 bar: ‚Novel Process Windows‘
10,000 t / aA = 4 x 106 l/(mol s) Ea = 5 x 104 J/mol412 Plates35 cm x 25 cm x 50 cm
1.7 Mio Euro
150 kEuro
March 2009
first comprehensive report: V. Hessel, P. Löb, H. Löwe, Curr. Org. Chem. 9, 8 (2005) 765-787
• Direct routes from hazardous elements
• Routes at increased concentration or even solvent-free
• Routes at elevated temperature and/or pressure
• Routes mixing the reactants ‘all at once’
• Routes using unstable intermediates
• Routes in the explosive or thermal runaway regime
• Process simplification – e.g. routes omitting the need ofcatalysts or (complex) separation
compare: Jähnisch, K.; Hessel, V. et al.; Angew. Chem. Intern. Ed. 43, 4 (2004) 406-446ACS group ‚Novel Chemistry‘, headed by Eastman Kodak
Hydrothermal high-temperature synthesis (Geochemistry Science 1991, 254, 5029, 231); superheated water processing (J. Org. Chem. 1994, 59, 3098; J. Org. Chem. 1997, 62, 2505); high-temperature ionic liquid processing (Org. Lett. 2005, 7 (19), 4205); solvent-free (Pure Appl. Chem. 2001, 73, (1), 193) and solvent-less (Chem. Comm. 2001, 2159) synthesis.
E. R. Murphy, J. R. Martinelli, N. Zaborenko, S. L. Buchwald, K. F. Jensen, Angew. Chem. 119 (2007) 1764F. B. Lopez, PhD thesis, High Pressure: a Challenge for Lab-on-a-Chip Technology, pp.137ff, University Twente (Reinhoudt group)
Excellence in Process Development Research AwardAIChE (New Orleans / USA, 2008)
NOVEL PROCESS WINDOWS
March 2009
New products via new process windows
• OLED materials
• Phenols by Kolbe-Schmitt synthesis
• Chitosan for Pharmaceuticals
• High pressure amination of hydorcarbons
• New ink materials
guided and accompanied by LCA & cost analyses
Universities in co-operation with industry: • Jenpolymers Ltd• Sigma-Aldrich• Heppe Medical Chitosan GmbH,• Pelikan PBS GmbH &CoKG• ASD GmbH, JTT
PROJECT CLUSTER „NOVEL PROCESS WINDOWS“ AT DBU
March 2009
Surfactant dispersion for liquidfabric enhancer productionVesicular dispersion
Aimed demo scale: 500 kg/h
Ionic liquid synthesisHighly exothermic single phase reaction
Aimed demo scale: 20 – 200 kg/d
Encapsulation processTwo step process, initial one dispersion
Aimed demo scale: increase of throughput by a factor of 10 compared to lab scale
Ozonolysis reactionGas/liquid contacting and reaction in a falling film reactor
Pilot scale: 10 l liquid/hProduction scale: about 100 – 1000 l/h
Suzuki-polycondensation for OLED material synthesisLiquid/liquid reaction
Production scale: several l/h
Case studies with IMM involvement
BMBF-project µ.Pro.Chem
BMBF-project POKOMI
PROCESSES CONSIDERED FOR TRANSFER FROM LABORATORY TO PILOT AND PRODUCTION SCALE
March 2009
x 10Labor
Pilot
Pilot
x 10Produktion
B. K. Vankayala, P. Löb, V. Hessel, G. Menges, C. Hofmann, D. Metzke, U. Krtschil, H.-J. Kost Int. J. Chem. Reactor Eng. 5 (2007) A 91
SCALE-OUT CONCEPTS FORFALLING FILM MICROREACTORS
March 2009
PILOT FALLING FILM MICROREACTORS IN PILOT PLANTS AT EVONIK-DEGUSSA
Ozone generator
Falling film microreactor of IMM for pilot scale
Ozone decomposition unit
Franke, R., Jucys, M., Löb, P., Rehfinger, A., Elements –Evonik Science Newsletter 2007, 22, 20.
BMBF-Projektµ.Pro.Chem
March 2009
• ½“ Tube, reactor consists of tube sections of varying length
• Adjustable reactor length (max. 1 m)
• Heating: tube-in-tube
cmPorosity: 95%
TWO DIFFERENT REACTOR CONCEPTS FOR SUZUKI COUPLING
Re-dispersion microstructured reactor
Metal foam filled tube reactor
March 2009
COPIRIDE - EU-PROJECT PROPOSAL (FP 7): NEW PLANT CONCEPTS
FABRICATIONCATALYSTS
REACTORS
PLANTS
PROCESSESOH
OH
OH
OH
COOHKHCO3 (aq)OH
OH
OH
OH
COOHKHCO3 (aq)
Cell-based common frame
plant
‘Container’
Block-based functional
module plant
MODULAR DEDICATEDDEDICATED
Hybrid integrated plant
High-pressure supercritical
plant
Ammonia Biodiesel
Fine chemistry
Volume: ~17 Mio €; Funding: ~11.0 Mio €
© IMM, March 2009
FABRICATION TECHNIQUES
© IMM, March 2009
MICRO-STRUCTURING TECHNIQUES- ETCHING
Wet chemical etching is an established techniquefor introducing microchannels into metal foils
Subcontractor: Herz Ätztechnik
© IMM, March 2009
MIKRO STRUCTURING – DEVELOPMENT OF PRODUCTION TECHNIQUES SUITABLE FOR MASS PRODUCTION
New Methods under Development:
EmbossingRolling
© IMM, March 2009
REACTOR PRODUCTION – DEVELOPMENT OF TECHNIQUES SUITABLE FOR MASS PRODUCTION
Established and suited for Mass Production:
Laser welding (at IMM)
New Methods under Development:Brazing Electron beam welding
© IMM, March 2009
MICRO-REACTOR TECHNOLOGIES FOR
DECENTRALIZED ENERGY GENERATION
© IMM, March 2009
MARKET FIELDS FOR FUEL CELLS
Mobile Application (Power train, Power Supply)
Residential Power supply; Emergency Power
Generation (Small scale stationary)
Power Supply (Stationary Power
Plants )
Hydrogen Filling Stations (Medium sized stationary
applications)
Portable Applications(Replacement of Batteries
and Generators)
Gasoline, Diesel, Methanol, Ethanol
Natural Gas
Natural Gas
Natural Gas; Ethanol
Methanol, LPG
© IMM, March 2009
Kolb, 2008
’Fuel Processing, Applications and Plants’, Wiley-VCH, Weinheim.
Power Generation Systems
- Small scale stationary (10 – 100 kW)
- Mobile Auxilliary Power Units (APU) for cars and trucks (5 – 20 kW)
- Mobile APU for caravans and yachts (< 1 kW)
- Portable for laptops (< 0.1 kW)
Drive Train
APPLICATION FIELDS OF MICROSTRUCTUREDFUEL CELL / FUEL PROCESSOR SYSTEMS
Kolb, Hessel, Review
Chem. Eng. J. 98, 1-38 (2004)
Hessel, Löwe, Müller, Kolb, 2005
’Chemical Micro Process Engineering - Processing, Applications and Plants’, Wiley-VCH, Weinheim, p.281 ff.
© IMM, March 2009
MOTIVATION FOR THE APPLICATION OF MICROTECHNOLOGY IN FUEL CELLS / FUEL PROCESSORS
Improved heat and mass transfer
Catalyst coating techniques similar to automotive exhaust clean-up
Low pressure drop (laminar flow regime)
Systemintegration – integrated heat-exchanger reactor design
Compactness – miniaturised heat-exchangers and evaporators
Improvement of system dynamics – fast start-up
Safety issues (microchannels act as flame arresters)
Kolb G., Hessel V, Review
Chem. Eng. J. 98, 1-38 (2004)
Hessel V., Löwe H., Müller, A., Kolb G., 2005
’Chemical Micro Process Engineering-
Processing, Applications and Plants’, Wiley, Weinheim
p.281 ff.
© IMM, March 2009
Truma Geraetetechnik GmbH & Co. KG, www.truma.de
Europe‘s largest manufacturer in the field of liquid gas heaters for leisure vehicles and boats.
Truma VeGA converts LPG into electricity!
“Truma is developing a fuel cell system that is specifically for the recreational vehicle area. With a view to the environment and efficient usage, we have put our faith in liquid gas as a fuel supply.“
Fuel Processor from IMM
250 W
Fuel: ca. 100 g/h LPG
Truma received the f-cell
award in silver 2007
THE TRUMA FUEL CELL SYSTEM – JOINT DEVELOPMENT
© IMM, March 2009
SYSTEM INTEGRATIONDIESEL APU 5 KWEL
5 kW Water-gas Shift Reactor
EU-Project Hytran – Hydrogen and Fuel Cell Technologies for Road Transport
© IMM, March 2009
ETHANOL STEAM REFORMING
WITH MICRO-REACTORS
© IMM, March 2009
PRICE OF BIO-ETHANOL
Sources: ‚Einsatz von Alkohol als Wasserstoffspeicher für Brennstoffzellenantriebe in Kraftfahrzeugen‘, R. Nußstein, 2000; www.impactlab.com, May 2004
Price of lignocelluloses biomass ethanol dropped from $1.62 to $1.20 per gallon (3.8 litre) during the last year.Cheaper alternative to gasoline.
(According to energy market research company “Industrial Information Resources”)
© IMM, March 2009
EXAMPLE OF BIO-ETHANOL COMPOSITION
Crude ethanol components Volume % Mole % (on a water free basis)
Ethanol 12.005 88.417 Lactic acid 0.998 5.713 Glycerol 0.994 5.868 Maltose 0.001 0.001 Water 86.002 Not applicable
This Composition is equivalent to a
Steam to Carbon S/C ratio of 3.
© IMM, March 2009
BIO-ETHANOL IN EUROPE AND THE US
Ethanol increasingly available in the US and EU: Ethanol additives in gasoline fuels.(2% by 2005 and 5.75% by 2010 in the EU)
2.8 billion gallons/year produced in the US through the fermentation of biomass.
Cost: ≈ $1/gallon competitive with petroleum fuels.
Significant cost issue of ethanol production: Water removal for gasoline fuel additive (distillation and zeolite adsorption).
Processing of ethanol for fuel cell applications does NOT require extensive removal of water.
Source: G. Santos, www.abengoabioenergy.com, June 2004
© IMM, March 2009
FUEL PROCESSING FOR FUEL CELL APPLICATIONS
Fuel tankPEM Fuel Cell
H2, H2O
CO2, CO, (N2)
H2, H2O
CO2, N2
SELOXor meth-anation
ReformerEvaporatorLT Water
gasshift
Water
Oxygen
HT Water gasshift
CCO [vol%]
MethanolReforming
≈ 1-1.5 < 10 ppm
Hydro-carbon Reforming
≈ 10 ≈ 3 < 1 < 10 ppm
Air
© IMM, March 2009
STR WGS PrOx 1
Compressor
Fuel Cell
HX HX
Afterburner
FCExhaust
Water
Evaporator
Exhaust
Fuel
Con-denser
CatalyticBurner
HX
REFORMING WITH MICROSTRUCTURED REACTORS – SPECIAL HEAT EXCHANGER FOR DIFFERENT PROCESS UNITS
Steam Reforming in Microstructured Reactors – Exemplary Process Scheme
System andDevice Integration
© IMM, March 2009
Reformer
Water
Fuel +Air
Combustion
Hydrogen from
Anode off-gas
Ethanol Water
Cathode
Off-gas
Combustion-gases
Reformate
Fuel tank
STEAM REFORMING IN INTEGRATED MICROSTRUCTURED HEAT-EXCHANGER REACTORS
Demonstrated for Methanol (A.Renken et al.; T < 300°C, IMM), Ethanol, LPG and Diesel (IMM; T ≥ 600°C)
© IMM, March 2009
POSSIBLE REACTIONS OF STEAM REFORMING (SR)
Ethanol steam reforming C2H5OH + H2O → 2CO + 4H2
Water-gas shift reaction CO + H2O → CO2 + H2
Side Reactions:
Ethanol decomposition to methane C2H5OH → CO + CH4 + H2
Ethanol dehydration C2H5OH → C2H4 + H2O
Ethanol dehydrogenation C2H5OH → CH3CHO + H2
Ethanol decomposition to acetone 2 C2H5OH → CH3COCH3 + CO + 3H2
Acetaldehyde decomposition CH3CHO → CH4 + CO
(Methanation CO + 3 H2 → CH4 + H2O)
Methane, acetaldehyde, acetone, ethene, are all undesirable products because they compete with H2 for the hydrogen atoms.
© IMM, March 2009
ETHANOL REFORMING CATALYSTS FOR H2 PRODUCTION
Extensive studies on hydrogen production from ethanol have been reported inthe literature:[Anthanasio et al. (2002, 2004), Breen et al. (2002), Cavallaro et al. (2003), Deluga et al. (2004), Freniet al., (2002), Galvita et al. (2001), Haga et al. (1998), Jose et al. (2003), Klouz et al., (2002) Leclerc etal. (1998), Liguras et al. (2004), Marino et al. (1998) and Velu et al. (2002)].
These authors have used catalysts such as:
Ni/MgO Cu/ZnO Cu/ZnO2 Pt/α-Al2O3Ni/Al2O3 Cu/Al2O3 CuO/ZnO/Al2O3 Rh/Al2O3Ni/La2O3 Cu/SiO2 Rh/Ce2O3Ni-Cu/SiO2 Cu/MgO Ru/Al2O3
Cu/NiO/Cr2O3Co/ZnO and Co/Al2O3.
Best performing were Ni/Al2O3, Ni/La2O3, Rh/Al2O3 catalysts.
There is very little or no research activity in the area of crude ethanol reforming
© IMM, March 2009
SANDWICH REACTOR APPLIED FOR CATALYST SCREENING AND TESTING
Wash-Coating of Etched Plates
Laser Welding
Catalyst Screening
Step 1: cleaning & thermal pre-treatmentStep 2: positioning & maskingStep 3: channel filling with suspensionStep 4: wiping-off excess suspensionStep 5: dryingStep 6: calcinationStep 7: pre-treatment of porous wash- coats (evacuation & pore filling with CO )Step 8: impregnationStep 9: drying & calcination
2
Process A: washcoating/wet impregnation
CO2Vacuum
CO2Vacuum
Step 7
CO2Vacuum
CO2Vacuum
Step 8 Step 9
Step 4 Step 5Step 3Step 2Step 1 Step 6
Process B: washcoating of commercially available catalyst powders (step 1 - 6)
e.g. Rh/Al O (DEGUSSA G 213 KR/D)2 3
Channel Dimensions: length 41 mm, width 500 µm, depth 2 x 400 µm
14 Channels per plate
600°C
Zapf, R.; Becker-Willinger, C.; Berresheim, K.; Holz, H.; Gnaser, H.; Hessel, V.; Kolb, G.; Löb, P.; Pannwitt, A.-K.; Ziogas, A., Trans IChemE A 81 (2003) 721-729
© IMM, March 2009
Thank you for your attention !SUMMARY OF TESTED CATALYSTS
Catalysts Metal loading [wt.-%]
Surface area [m2/g]
Co/Al2O3 10 161 Co/SiO2 10 165 Co/MgO 10 177 Co/ZnO 10 12 Ni/Al2O3 10 156 Ni/MgO 10 70 Rh/Al2O3 5 149 Rh/MgO 5 58 Ru/Al2O3 5 149
Rh/Ni/Al2O3 5/10 125 Rh/Ni/CeO2/Al2O3 5/10/15 170
Rh/Co/Al2O3 5/10/15 164
Men, Y., Kolb, G., Zapf, R., Hessel, V., Löwe, H.;"Ethanol steam reforming in a microchannel reactor", Chem Eng. Res. Des. Dev.. 85, B5 (2007) pp. 1-6.
© IMM, March 2009
Thank you for your attention !ETHANOL STEAM REFORMING – CATALYST PERFORMANCE – BIMETALLIC CATALYSTS
Higher conversion of bimetallic catalysts at low temperature
most active and selective Rh/Co catalysts
0
10
20
30
40
50
60
70
80
90
100
350 400 450 500 550 600 650
Temperature [oC]
Etha
nol c
onve
rsio
n [%
]
Rh(5%)/Al2O3
Rh(5%)/Ni(10%)/Al2O3
Rh(5%)/Ni(10%)/CeO2(15%)/Al2O3
Rh(5%)/Co(10%)/Al2O3
© IMM, March 2009
Thank you for your attention !
Full conversion at 400 oC
Low ethylene and acetaldhyde selectivity
ETHANOL STEAM REFORMING – CATALYST PERFORMANCE – BIMETALLIC Rh/Co/Al2O3 CATALYSTS
© IMM, March 2009
Stable for 130 hrs 650 oC
DURABILITY TEST OF Rh/Co/Al2O3 CATALYSTS
© IMM, March 2009
CONCLUSIONS CATALYST DEVELOPMENT
Primary screening of monometallic (Co-, Ni-, Rh-) and bimetallic (Rh/Ni and Rh/Co) catalysts
monometallic catalysts: Rh most active
Superior activity of bimetallic Rh/Ni and Rh/Co catalysts
Highly active and stable Rh/Co/Al2O3 catalyst
Further work on lowering Rh content while maintaining high activity
© IMM, March 2009
DESIGN OF PROTOTYPE BURNER-INTEGRATED REFORMER - 250-500 KWEL POWER EQUIVALENT -
electr. heating (start-up)
Reformer inlet
Reformer outlet (to burner)
Burner inlet (from burner)
Burner outletReformer / Burner
Co/ZnO-Catalyst (LIKAT) incorporated into the reactor
© IMM, March 2009
INTEGRATED ETHANOL STEAM REFORMER / CATALYTIC BURNER (250 W)
Part of the work presented here was funded by the Deutscher Bundesstiftung Umwelt (DBU) AZ 22420-31
© IMM, March 2009
INTEGRATED REACTOR – SELECTIVITIES VS. LOAD LEVEL INTEGRATED REACTOR – CONVERSION VS. LOAD LEVEL
0
10
20
30
40
50
60
70
20 30 40 50 60 70 80
Loadlevel [%]
S (C
H 4, C
O2,
CO
, CH 3
CH
O) [
%]
S(CH4) [%]S(CO2) [%]S(CO) [%]S(CH3CHO) [%]
60
65
70
75
80
85
90
95
100
20 30 40 50 60 70 80Loadlevel [%]
X C
2H5O
H [%
]
X C2H5OH[%]X C2H5OH[%]
S/C = 2
S/C = 3
© IMM, March 2009
FUEL PROCESSING IN MICROSTRUCTURED REACTORS - EXEMPLARY PROCESS SCHEME: ETHANOL STEAM REFORMING -
System Pressure: Atmospheric
Feed Composition: 44,72 Vol. % C2H5OH,
55,28 Vol % H2O (S/C=2,0)
Gas Purification of Reformate by Water-gas shift (WGS) and Preferential
Oxidation (PrOx)
Fuel Cell: Low Temperature-PEM-Fuel Cell
70% H2-Utilization
50% Electrical Efficiency
Utilization of Anode Off-gas and Heat of WGS and CO PrOx Reactions
Reformer Operating Temperature: 600°C at S/C=2.0
© IMM, March 2009
FUEL PROCESSING IN MICROSTRUCTURED REACTORS - EXEMPLARY PROCESS SCHEME: ETHANOL STEAM REFORMING -
© IMM, March 2009
CONCLUSIONS
Liquid fuels offer numerous advantages for future distributed power generation (portable, mobile and small scale stationary)
Ethanol is one of the few options for future sustainable liquid fuels
Future catalyst technology for ethanol reforming should allow for moderate operating temperatures (below 500°C)
Microstructured plate heat-exchanger reactors offer unique opportunities of size reduction and system integration. Novel process routes may be pursued
© IMM, March 2009
Thank you for your attention!!
