RESEARCH POSTER PRESENTATION DESIGN © 2015

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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