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Crude Oil and Asphaltene Characterization
Published in Francisco M. Vargas, Mohammad Tavakkoli, Asphaltene Deposition, 2018
R. Doherty *, S. Rezaee *, S. Enayat, M. Tavakkoli, F. M. Vargas
The solution of solvent and resins leaving the clay column is fed into the distillation column from the top side and is collected in a round-bottomed flask. The heating mantle maintains a temperature of around 321 K (118°F). At this temperature, the solvent evaporates and leaves the column as a vapor without burning the resins. At the top of the distillation column, there is a thermometer, which should always indicate a temperature very close to the boiling point of the solvent to ensure that the vapor is pure solvent. Solvent as a vapor continues its path across the condenser. Cold water is used to condense the vapor into a pure liquid solvent, which is collected in the solution container. The same distillation process is followed for the aromatics leaving the silica gel column. Once the columns are completely cleaned with no residues of resins or aromatics, the distillation is stopped, and both resins and aromatics are dried in an oven and are then weighed. Figure 2.6 shows the crude oil and the SARA fractions separated from the crude oil by the automated chromatographic columns system (Rezaee et al. 2017a).
Process intensification studies in synthesis of biodiesel with a helical coil continuous microreactor
Published in Biofuels, 2023
Sravanthi Veluturla, Shriya Anand Rambhia, Sindhu Pranavi
The transesterification for the production of biodiesel was done using sunflower oil, methanol and KOH as the catalyst. The experimental setup used in the present research is schematically illustrated in Figure 1. The apparatus encompasses a syringe pump, helical coil reactor, T-joint mixer, and heating mantle with temperature control and oil bath. The microreactor used in this experiment is a helical coil with internal diameter of 0.8 mm and length of 2 m. In terms of experimental conditions, the residence time was varied from 1 to 3 min, the molar ratio of reactants varied from 3:1 to 9:1 (methanol:oil) and a catalyst loading of 0.5 to 1.5 wt% was used.