Sản xuất biodiesel từ nguyên liệu vi tảo Spirulina sử dụng trực tiếp gần điều kiện metanol siêu tới hạn
Biodiesel Production from Spirulina Microalgae Feedstock Using Direct Transesterif ication Near Supercritical Methanol Condition Reporter: Tran Thanh Phuc Lecturer: Do Quy Diem, PhD Outline • • • • Introduction Materials and methods Results and discussion Conclusions INTRODUCTION BIODIESEL INTRODUCTION INTRODUCTION Spirulina Microalgae Alcohol in the presence of an alkaline catalyst • High productivity of lipid • Non-eatable source • High growth rate • Growth in water (freshwater or seawater) • Environmental benefits of diminishing CO2 from air • Bioremediation of wastewater from pollutants BIODIESEL INTRODUCTION Drawbacks direct transesterification Lipid extraction from biomass is difficult Drawbacks Separation of used catalyst from products and treatment of wastewater Supercritical in-situ transesterification • • Simple and has the advantages regarding environmentally-friendly properties, high conversion within a short time, No need for using acid or base catalysts and so consequently, no need for post treatment INTRODUCTION Supercritical Any substance at a temperature and pressure above its critical point Distinct liquid and gas phases not exist Critical point • • It can effuse through solids like a gas, and dissolvematerials like a liquid The molecules in the supercritical fluid have high kinetic energy like a gas and high density like a liquid MATERIALS AND METHODS MATERIALS AND METHODS The reactor was heated with an electric heating jacket while the temperature was sensed using a thermocouple Pressure was fixed at equilibrium pressure of 12MPa in all the experiments The impact of biomass was neglected Interaction parameters in SRK EOS between methanol and n-Hexane, methanol and water, and nHexane and water was obtained 0, -0.9 and 0.51090, using Aspen-Hysys software databank Temperature and pressure of n-Hexane is lower than methanol Tubular batch reactor Tecrease the critical temperature and pressure of the system MATERIALS AND METHODS The reactor was brought out of the heating jacket and was immersed into an ice water FAMEs and n-Hexan Filtered Methanol, glycerol and other polar Segregated and retained compounds Washed FAMEs are transferred to n-Hexane phase Transferred to separatory funnel GC-MS BIODIESEL RESULTS AND DISCUSSION Experimental conditions and alkyl esters yields Methanol- to-dry Co- solvent- to-dry algae algae 40 275 20 250 Run order Temperature Time 275 Critical Pressure Moisture content Critical Temperature (oC) 20 240.89 5.50 29.92 10 60 248.54 7.77 24.89 30 40 249.14 8.78 11.32 225 40 10 60 248.54 7.77 3.68 225 40 10 20 240.58 6.09 8.46 300 30 40 244.88 6.61 99.32 275 40 10 20 242.35 7.31 73.49 250 30 4 40 247.48 5.97 11.33 275 40 60 252.56 7.63 95.75 (Mpa) FAME yield (%) RESULTS AND DISCUSSION Methanol-to-dry microalgae ratio effect RESULTS AND DISCUSSION Hexane-to-dry microalgae ratio effect The presence of additional n-hexane as a co-solvent had a negative impact on the efficiency of biodiesel production In supercritical condition, methanol plays as solvent in addition to its reactant role No need for another solvent and the additional solvent just reduces the concentration and density of the reactants RESULTS AND DISCUSSION Moisture content effect (2) Water can form a hydrated layer around (1) Fatty acid methyl ester production reaction is a the biomass and prevent the lipid from bulk reversible reaction and water can reverse the releasing into the reaction medium esterification reaction toward methanol and free fatty (3) Triglyceride hydrolysis reaction may acid production occur instead of transesterification reaction Increasing percentage of humidity fatty acid methyl ester yield decreased CONCLUSIONS Maximum yield of 99.32% in comparison with the reference method Study various aspects of biodiesel production, by the method described, in order to reduce operating costs and industrialize this procedure can be considered as future work