Abstract 1. The experimental viscosities densities measured with Anton Paar SVM 3000 equipment, and refractive indices measured with Refractive Meter equipment, corresponding values of excess molar volumes (VE ), deviations in viscosity (Δμ), deviations in refractive index (ΔnD), excess Gibbs energy (GE), and excess molar enthalpy (HE), for binary, ternary and fourth mixtures of alcohol, ether, and n-alkanes. 2.Used for the calibration experimental from paper [7] were the mixture for the binary system (tert butyl alcohol + ethanol ), we had good result and ADD% for densities, viscosities and refractive indices were 0.1657 %, 0.4846 %, and 0.033545 % respectively. 3.Data of binary mixture were fitted to a Redlich-Kister's The choice of the proper number of coefficients (p), was based on the standard deviations, and the F-test as criterion of goodness with an error lower that 1% see. 4.Data of ternary and fourth mixture were correlated by Cibulka equation were determined with the optimization algorithm similar to that for the binary parameters the σ values was less than 0.05%. 5.The experimental viscosities densities and refractive indices were positive and decrease with increase temperature for all tables for binary ternary and fourth mixtures. 6.Excess molar volumes (VE), was negative value for all binary system, Deviations in viscosity (∆µ), negative value, but at system (n-hexane + n-heptane), maximum positive and minimum with negative value, Deviations in Refractive Index (ΔnD), was were positive for all binary mixtures, Excess Gibbs Energy was negative for all binary ,but maximum positive and minimum with negative value just at system (n-hexane + n-heptane). 7.Excess properties for ternary mixture negative and positive value. 8.Excess properties for fourth mixture negative value.
سهير المبروك دربال (2009)

Abstract Against the background due to the energy crisis in the late 1970’s, the pinch analysis has emerged as a powerful tool for the integrated design of process heat networks which include heat exchangers, distillation columns, furnaces, etc..The key strategy of this methodology is to set energy targets prior to design based on basic thermodynamic principles.The subject of this thesis in to apply this analysis to one of the Libyan Refineries, namely Ras Lanuf Refinery, to assess energy utilization of such big energy – consuming plants and to explore the potential of energy as well as capital costs savings based on the finding of applying this analysis. Based on actual operating data collected from the plant and application of the procedure of the pinch analysis to this real case study where a minimum temperature difference approach in the Ras Lanuf refinery heat exchangers design of 10 (ΔT min =10 ) the following results were obtained. Actual rate of energy consumption of the base case design of the refinery is 9MW which is provided by burning fuel oil in the furnace, while the minimum target predicted by the pinch analysis should be 8MW. This amounts to just over 11% energy savings which equivalent to $462,000 per year reduction in the operating cost of the refinery
هويدة الهادي الحبيشي (2011)

Abstract This research was an attempt to use the currently available activity coefficient methods with universal sets of parameters to simultaneously predict ternary liquid-liquid equilibrium data. The focus of this research was to calculate phase equilibrium data within fair error using set of Parameters obtained from the above-mentioned models. The significance of this work is to study the liquid-liquid phase equilibrium of the ternary system at several temperatures and to test the capability of the various equilibrium models to correlate these data. A series of liquid-liquid equilibrium measurements were performed by changing the composition of the mixture.The prepared mixtures were placed in the extraction vessel and stirred for 2 h and then left to settle for 4 h. Samples were taken by a syringe from both the upper phase and lower layers. Both phases were analyzed using gas chromatography equipped. Liquid-liquid equilibrium for the ternary system acetonitrile + benzene + n-heptane was measured at 298,313,333 K. The results were used to estimate the interaction parameters between each of the three compounds for the NRTL and UNIQUAC models as a function of temperature. The estimated interaction parameters were successfully used to predict the equilibrium compositions by the two models. The UNIQUAC equation was the most accurate model in correlating the overall equilibrium compositions of the studied system. NRTL models satisfactorily predicted the equilibrium compositions. In each of the mentioned the ternary system, the calculated and experimental data were compared. The root mean square deviation (RMSD) between the observed and calculated mole percent for NRTL, UNIQUAC was 1.44%, 1.35% for acetonitrile + benzene + n-heptane
عماد الدين محمد الزغداني (2014)