The Future of Energy with Agricultural Carbon Utilization

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Bethany Dean
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1 The Future of Energy with Agricultural Carbon Utilization Energy & Agricultural Carbon Utilization Symposium (June 11, 2004) Athens, GA Danny Day, Eprida James Lee ORNL (Oak Ridge, TN) Don Reicosky USDA Soil Conservation (Morris, MN) Matthew Realf and Ling Zhang Georgia Institute of Technology (Atlanta, GA) 1

2 Pyrolytic conversion offers cost effective options The 2001 report by Spath * offered that pyrolytic conversion of biomass offered the best economics for hydrogen production, partly because of the opportunity for co-product production and reduced capital costs. *Spath, et al, Update of Hydrogen from Biomass -Determination of the Delivered Cost of Hydrogen, National Renewable Energy Laboratory, Milestone Report for the U.S. Department of Energy s Hydrogen Program

3 Drivers for sustainable biohydrogen production Energy Independence Dwindling Oil Reserves Global Warming Distributed Socio-Economic Impacts Ability to co-locate and integrate unrelated business, symbiotic processing 3

4 Current uses of Hydrogen Uses non renewable hydrogen Synergistic opportunities for renewable hydrogen can be found in hydrogen s largest use Under intensive modern agriculture Hydrogen = Food Agricultural Fertilizer Oil Refineries Methanol Chem-Proc, Other Space Programs 4

5 Background Demonstration of Hydrogen Production A 3 year DOE/NREL project resulted in a pilot demonstration of hydrogen from biomass. The aim was to safely operate a continuous process catalytic steam reformer to process the oxyhydrocarbon gas from biomass pyrolysis and capture 24 hours of stable data. Peanut hulls pellets were heated with natural gas in an oxygen free system, producing an off-gas rich in hydrogen. The steam reformer was externally heated to 850C. Prior to Insulation Initial Test Run Pyrolysis Reactor Steam Reformer Reactor 5

The online monitoring recorded by weight production rates of : 60% H2 3% methane (giving the hydrogen a blue flare) 30% CO2 7% CO During this run the process also sequestered 20% of the biomass as

6 Demonstration Results A 100 hour run was planned to insure that a stable 24 hour window of data was collected after processes had stabilized. Throughput was set at 50kg/hr of biomass with a moisture content of 13%. The online monitoring recorded by weight production rates of : 60% H2 3% methane (giving the hydrogen a blue flare) 30% CO2 7% CO During this run the process also sequestered 20% of the biomass as fixed carbon. The variations in the run conditions produced three different types of char. An accidental discovery in start-up pointed toward a new application. Hydrogen Flare Pyrolysis Flare Stable operating conditions: 24 hour duration from hours into the run :00 25:30:00 39:40:00 52:20:00 64:50:00 77:20:00 91:00:00 103:40:00 116:40:00 129:10: Time in Run Feed total 15 per. Mov. Avg. (Out Gas Temp) 15 per. Mov. Avg. (low er cgar:process Variable( C)) 15 per. Mov. Avg. (burner box) 15 per. Mov. Avg. (py dp x 500) 15 per. Mov. Avg. (side mid 2) 15 per. Mov. Avg. (TSI610A:Bed heater ( C )) 15 per. Mov. Avg. (Burner Lambda (VOLT METER #1)) 14 per. Mov. Avg. (Lambda Gas Out (VOLT METER #2)) 15 per. Mov. Avg. (Feed temp:process Variable( C)) 15 per. Mov. Avg. (Educ. stm. (no ctrl):process Variable( C)) 15 per. Mov. Avg. (h2 flare:process Variable( C)) 15 per. Mov. Avg. (PDI610:PV( KPA) x100) 15 M A (h2 fl P V i bl ( C))

7 Low Temp Charcoal Advantage Ammonia adsorption on Charcoal 7

8 Integrated System with H2 and Ammonia from Biomass Pyrolysis System Steam Reforming System Water Steam Superheating O2 Biomas s Biomass Preheating Pyrolyzer Bio-oil Bio-oil Preheating Steam- Reforming Heat Recovery I PSA Off-gas Combustion Char N2 H2 H2O CO2 Heat Recovery II Ammonia Production System Product Mixture Syngas Preheating Product Mixture Recycle Separator NH3 Ammonia Converter Compressor 4 Compressor 3 Compressor 2 Compressor 1 Final Cooler Cooler 3 Cooler 2 Cooler 1 8

Process Flow : Hydrogen Production and CO 2 Sequestration Producing an Enriched Carbon Organic Slow

Reactor H 2 + CO 2 Steam Steam Reformer H 2 (1x) CO 2 Pressure Swing Adsorption H 2 (3x) Use/Sell

Sequestered Carbon Fossil Fuel Gases w/ CO 2 /SO x /NO x Profit Centers Char Oxy-Hydrocarbon Gas

9 Process Flow : Hydrogen Production and CO 2 Sequestration Producing an Enriched Carbon Organic Slow Released Fertilizer (Patent Pending) -Forest Residue -Energy Crops -Carbon Sources Pyrolysis Reactor H 2 + CO 2 Steam Steam Reformer H 2 (1x) CO 2 Pressure Swing Adsorption H 2 (3x) Use/Sell Purifier/Dryer Compressor Heat Exchanger Optional Reuse w/o Fossil Fuel N 2 Catalytic Converter 20% Sequestered Carbon Fossil Fuel Gases w/ CO 2 /SO x /NO x Profit Centers Char Oxy-Hydrocarbon Gas Water Char Fluidized Cyclone Revenue Sources Recycling Pump Ammonia Condenser ECOSS Fertilizer Clean Exhaust 9

10 Operated at ambient pressure and temperature CO2 separation is not required Pilot Test 30 Min Granular Original Char 15 Min sand like 10

started inside the carbon structure After complete processing,

11 Crushed Interior 2000x SEM The residual cell structure of the original biomass is clearly visible The ABC fibrous buildup has started inside the carbon structure After complete processing, interior is full Trace minerals are returned to the soil along with essential nitrogen. 11

12 Carbon Negative Energy Carbon Dioxide per GJ of Various Fuels B it uminous Diesel Gasoline Fuel Propane LPG Natural Gas Solar Pv (mean) Carbon Negative Energy U.S. EPA CO2 kg / GJ 12

13 Frames of reference 13

14 Our Future: Integrated Systems 14

Hydrogen from Biomass Pyrolysis: Integrated Co-Products and Services

Hydrogen from Biomass Pyrolysis: Integrated Co-Products and Services Biorefining Videoconference (June 17, 2004) Danny Day, Eprida danny.day@eprida.com 716-316-1765 James Lee ORNL (Oak Ridge, TN) Don Reicosky