Presentation Transesterification Reaction Design

1. Integrated solar-biomass technology for production of green power and products Chris Leech, Cody Cleaver, Ahmad Majzoub , Warren Furnival , Helen Lockhart University of Western Ontario Department of Chemical and Biochemical Engineering CBE 4497 Plant Process and Design

2. PFD Section 300 - Biodiesel Production

3. Transesterification FAME Glycerol WVO Methanol

4. Innovation of Biodiesel Production Glycerol-based fuel additive assists Decreasing in particulate emissions Act as cold-flow improvers Viscosity reducer

5. CSTR C57H104O6 + 3CH3OH ↔ 3C19H36O2 + C3H5(OH)3 Total Volumetric Flowrate = 18,500 L/day Residence time= 2.2 hrs

6. CSTR practical issues, key design considerations/challenges Potential Problems Problem with high viscosity in algal oil when being treated Formation of acrolein highly toxic substance formed by thermal decomposition of Glycerol Glycerol-based fuel additive increases biodiesel quality/commercial value Substrate used is Isobutylene Etherification is the transformation process Catalyst used: Amberlyst-15 Benefits

7. Environmental Assessment M inimizing environmental impact of waste streams Only one waste stream: waste water Our methanol is fully recycled and reused Glycerol utilized as fuel additive instead of waste stream

8. Alternative CSTRs considered CSTR vs Batch Reactor Utilizing methanol vs ethanol as alcohol Membrane vs Centrifuge Not influenced by FFA Saponification Not used commercially Sensitivity to purity of reactants Research Slower reaction

9. CSTR assumptions Assumptions 97% conversion is achieved Recycled vent gasses are mostly methanol Reference temp.= 25 o C (298.15K) Cp values calculated with empirical formulas 2:1 height to diameter ratio Plant height restriction at 5 m

10. Detailed Design Calculations H:D ratio is 2:1, or R = 2 Where V is the volume (m 3 ), and t he height H is given by:

11. Detailed Design Calculations The power requirement [ W] : Therefore, the number of impellers (N i ,rpm) was found using the correlation given in Haynes (2004): Where k 2 is the proportionality constant, ρ is the average fluid density, and D i is the impeller diameter.

12. CSTR Reactor CAD Design

13. CSTR sketch/dimensions/internals Volume of reactor = 12.6 m 3 Conical shape for bottom of reactor volume =0.5 m 3 ,height = 0.5 m and diameter = 2 m Unit Cost: $59,800 Width of baffle: 0.09 m Type of Impeller: Rushton Turbine Baffles: Carbon Steel Type 405 Blades: Carbon Steel Type 410 Material: Austenitic Stainless Steel (IS: 1570-1961) Wall thickness: 135.91 mm

14. Process and Instrumentation Design Simple Feedback Top Control Flow controller for Algal Oil/Methanol/WZA volumetric flow Level Controller utilized to prevent overflow Temperature Transmitter maintains temp. at 65C Supervisory Process Control allows all units to relay information to Process Logic Controller Pneumatic valves set up for temp. and pressure regulation

15. Innovation in Biodiesel Production Glycerol-based fuel additive assists Decreasing in particulate emissions Act as cold-flow improvers Viscosity reducer Commercial Value for: Biodiesel reformulation Octane booster Decrease cloud point of diesel fuel when blend with biodiesel

16. Economic Analysis Total Equipment Cost $13,162,500 Total Capital Investment $11,210,000

17. Profitability Price $/tonne Price USD FAME 868.21 7,000,000 Glycerol 680.00 710,000 Tax Exemptions 200.35 1,603,000 Annual Sales Revenue $9,250,000 Price $/gallons FAME 2.95 Glycerol

18. Profitability Expenses Direct 5,690,000 Indirect 443,000 General 1,030,000 Annual Total Expense $7,160,000 Annual Net Income 2,080,000 Payback Period 5.4 years Return on Investment 18.6%