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RESEARCH POSTER PRESENTATION DESIGN © 2015
www.PosterPresentations.com
PROBLEM STATEMENT & SCOPE OF PROJECT TECHNO-ECONOMIC ANALYSIS
Table 1: Feed Composition and Conditions
Figure 1: Bioconversion Process Overview
The Bioconversion of Lignocellulosic Biomass to Fatty Alcohols
Rose Holbrook, Michael Buckner, Matthew Cackovic, James McCall, Michael SteinAdvisor: Jennifer Markham
Figure 3: Piping & Instrumentation Diagram
Figure 4: Gantt Chart for Bioconversion Process & Reactor Schedule
SUMMARY
SENSITIVITY ANALYSIS
The purpose of this project is to minimize the production cost of fatty alcohols using a biological
synthesis pathway.
Solubilized Hydrolysate356000
Insoluble Solids (IS) <0.05%Soluble Solids (SS) 15%
43Pressure [atm] 1Vapor Fraction 0
Free Fatty Acids (FFA) 0Water 303000Glucose (SS) 29300Xylose (SS) 16100Other sugars (SS) 4000
Figure 5: Object Oriented Code Structure
Reactor EffluentDodecanol (C12H26O) 5,120Tetradecanol (C14H30O) 5,120Carbon Dioxide (CO2) 27,400Water (H2O) 70,600Cellular Solids (C5H7O2N) 20,800
Bicarbonate (HCO3-) 935
Ammonium (NH4+) 276
Glucose (C6H12O6) 2,430Oxygen (O2) 144Total 133,000Table 2: Feed Composition and Conditions
Figure 2: Dodecanol (Fatty Alcohol) Chemical Structure
• Mechanical vapor recompression evaporators (x4)• Agitated, aerated bioreactors (x20)
• Incremental seed reactors (x5)• Centrifuge (x16)• Filter
Equipment Used
Global Selling Price: $2.50/kgRequired Minimum Selling Price:
$4.25/kg* * Best case scenario
Figure 6: Cost Contributors
3 C6H12O6 →6 CO2 + 5 H2O + C12H26O
7 C6H12O6 → 14 CO2 + 12 H2O + 2 C14H30O
0.0125 O2 + 0.03748 C6H12O6 + 0.0425 HCO3- +
0.0425 NH4+→0.1825 H2O + 0.055 CO2 + 0.0425
C5H7O2N
PROCESS SIMULATION & DESIGN
RESULTS
Reactor SpecificationsReactor Q (m3/hr) 97.2Min. Volume (m3) 11,539
Turnaround Time (hr) 10Accumulated Vol. over turnaround time (m3) 972
Total Volume (m3) 12,500Total # of reactors 20Reaction time (hr) 129Residence time (hr) 119
• Lignocellulosic biomass is an abundant and mostly underutilized source for fermentable sugars produced via hydrolytic conversion.
• Fatty alcohols can be used as detergents, industrial solvents, emulsifiers, and may be further refined into biofuels.
• Currently, most fatty alcohols are derived from palm kernel oil, coconut oil, or petrochemical sources (sustainability issues).
• Process: lignocellulosic hydrolysate → (genetically modified microorganism) → fatty alcohols
• Economic sensitivity analysis was conducted to determine the factors affecting the selling price and production costs
Table 3: Reactor Specifications
Purchase Cost
Operating Cost
Utilities Cost
MSP vs Feed Cost
Y=5.3x+2.4
MSP vs Productivity vs Yield (gal)
MSP vs Productivity vs Yield (kg)
Number of Reactors vs Productivity vs Yield
Yield
Yield
YieldProductivity
Productivity
Productivity
MSP ($)
MSP ($)
MSP ($)
MSP ($)
Feed Cost
Compressor
EvaporatorHeat X
Reactors
Reactor AerationSeed ReactorsCentrifuge
Reactors
CompressorCentrifuge
Seed Reactors
Feed Cost / YearGeneral Admin ExpensesSolids
TreatmentTax / InsuranceOverhead
Maintenance
Labor
Utilities
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