Industrial production of vegetable oil from palm kernel seed operational process was analysed in this research study with the extractor unit as the main focus of the study. The extractor unit consist of nine operational stages, which was modeled by applying the principle of the law of conservation of mass and energy respectively. The developed models were a set of ordinary differential equations, which were solved by using MatLab ODE 45 solver by applying industrial extractor plant data of Vegetable Oil Production Company. The developed models' results were compared with the industrial extractor plant data in terms of mass fraction of oil and temperature of the raffinate and mass fraction of oil and temperature of the extract and these yielded an absolute percentage error (deviation) of 7.0, 9.52, 3.29 and 2.29 respectively. Thus, the deviations are within the acceptable limits, which shows that the developed models predicts adequately the extraction process of vegetable oil production. In addition, the effects of mass flow rates of raffinate and extraction solvent were studied with increase in mass flow rate of raffinate reduces contact time between extraction solvent and the cake thereby reducing the efficiency of the extraction process with maximum amount of oil been extracted at the minimum flow rate of 300Kg/hr.
The study aimed at availability of petroleum products in Nigeria through the operation of enhanced modular refinery process due to inefficient conventional major refineries. The enhanced modular refinery converts or processes residue product from conventional modular refinery as feedstock to the hydrocracker reactor for viable and desired products such as liquefied petroleum gas, naphtha and diesel. Therefore, twenty Nigerian crude oil types were classified as sweet, light and medium crude oil, and these crude oil types were categorized based on their recovery volume at true boiling point of 370oC as Group A, Group B and Group C respectively. Thus, based on product output and equipment cost, a modular refinery with 29 trays was used in this study, as light and medium sweet crude oil types were simulated in a modular refinery of various column trays prior to the desired tray. A topping plant with a 30,000 barrel per day capacity and a modified topping plant with 29 trays respectively were used to process different types of Nigerian crude oil. using Aspen Hysys to evaluate their products yield and tray compositions. The modified modular refinery with hydrocracker yielded more valuable from the residue of conventional modular refinery with minimal bottom fraction. Performance models for hydrocracker reactor was developed based on the nature of reaction, kinetic parameters estimated and results compared with experimental data with minimum deviations. The developed performance models predicted feedstock conversion and product yield along the hydrocracker reactor’s dimensionless length by solving a set of ordinary differential equation models. Thus, the hydrocracking process was simulated to evaluate the effects of catalyst effectiveness factor on feedstock conversion and products yield.
Models for carbondioxide methanation in a packed bed reactor was developed from first principles by the application of the law of conservation of mass and energy. The kinetic expressions of the process where obtained from relevant literatures and incorporated and solved simultaneously with the developed models using Matlab ODE45 solver. Sensitivity analysis was performed to ascertain the optimal conditions gave reasonable results, which were validated with plant data and was found to be accurate with deviations within allowable range. The research study focuses on carbondioxide methanation reaction for production of synthetic natural gas (SNG) and the performance of the process is characterized by carbondioxide conversion under various operating conditions. One dimensional pseudo-homogeneous packed-bed reactor model neglecting all possible mass and heat constraints was used as a reference and the resulting model equations are solved numerically. The reaction rates and exothermicity (∆H°=-165KJ/Mol) prevent a packed bed reactor to be operated at high conversions and the reactant inlet temperature is used as a primary parameter, while an optimum inlet temperature is determined at which the carbondioxide conversion has maximum value. With inlet temperature higher than the optimum temperature, CO 2 conversion decreases due to the reverse Sabatier reaction.
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