Badie I. Morsi - Academia.edu (original) (raw)

Papers by Badie I. Morsi

IntechOpen eBooks, Nov 2, 2022

Journal of Petroleum & Environmental Biotechnology, Jan 7, 2014

The presence of azeotropic points in the vapor-liquid equilibria of some solutions is a limiting ... more The presence of azeotropic points in the vapor-liquid equilibria of some solutions is a limiting factor in separation operations by distillation. Knowledge of azeotropy is based on understanding its origins and behavior in relation to the different variables that modulate phase equilibria, and can be used to control the appearance of these singular points. This work studies the phenomenon of azeotropy and presents a practical view based on the study of ester-alkane binary solutions. After considering the principles of vapor-liquid thermodynamics and the special cases of azeotropic points, a detailed description is given of the experimental techniques used to determine these points and also for their thermodynamic verification. Two different but complementary modeling approaches are proposed: the correlation of experimental data and the prediction of azeotropic variables. The first is required to achieve a rigorous design of apparatus and installations, while the second is useful in preliminary design stages. Finally, alternatives to the separation process are studied by simulation. For a practical perspective on these aspects, each section is accompanied by data for ester-alkane solutions, and references are made to applications in the chemical, food and pharmaceutical industries.

HAL (Le Centre pour la Communication Scientifique Directe), Apr 14, 2022

International Journal of Coal Preparation and Utilization, Feb 1, 2016

ABSTRACT This article presents an extensive review of the coal-agglomeration process, including o... more ABSTRACT This article presents an extensive review of the coal-agglomeration process, including oil-agglomeration theory, characterization methods of coal hydrophobicity, and the main factors affecting the agglomeration-process performance in terms of combustible recovery and ash rejection. Coal rank and oxidation state, coal petrography and composition, coal-particle size, pulp density, and pH, bridging-liquid type and concentration, presence of surfactant and electrolytes, bridging-oil emulsification, and agitation intensity as well as time are among the factors here discussed. A chronological overview of the development and milestones of the coal-agglomeration processes is also provided.

International Journal of Chemical Reactor Engineering, Jun 18, 2013

The hydrodynamics (gas holdup, Sauter mean bubble diameter, d 32) and the overall volumetric liqu... more The hydrodynamics (gas holdup, Sauter mean bubble diameter, d 32) and the overall volumetric liquid-side mass transfer coefficients (kLa) were measured in a large-scale (0.29 m ID, 3 m high) slurry bubble column reactor (SBCR) for He/N2 gaseous mixtures, as surrogates for syngas, in three different Fisher–Tropsch (F-T) products (liquid paraffins mixture, light F-T cut and heavy F-T cut) in the presence and absence of three different solids (spent iron oxides catalyst, alumina powder and Puralox alumina). The effects of pressure (10–30 bar), temperature (up to 500 K), superficial gas velocity (0.14–0.26 m/s), solid concentration (0–20 vol.%) and gas density on these design parameters were investigated. The experimental data revealed that increasing the reactor pressure or gas density increased the gas holdup and decreased d 32, by increasing the population of the small gas bubbles, which increased the overall kLa values for all the gas mixtures used in the three F-T cuts under most of the operating conditions employed. Increasing temperature increased the gas holdup in the three F-T cuts, except for N2-light F-T cut, where the gas holdup values remained almost constant from 400 to 500 K. Increasing the slurry concentration decreased the gas holdup and increased d 32, mainly for gaseous mixtures with high He mole fractions, which decreased the overall kLa under all conditions used. Increasing the gas superficial velocities (UG ) increased the gas holdup and kLa values, even though d 32 was found to increase or decrease with increasing UG . Increasing the He mole fraction in the He/N2 gaseous mixture at constant pressure led to low gas holdup and high d 32 which decreased kLa values, and under similar operating conditions, kLa values of He as a single gas were always lower than those of N2 as a single gas. Increasing the He mole fraction in the He/N2 gaseous mixture at constant density, however, was found to have negligible effect on the gas holdup, d 32 and subsequently on the overall kLa. The gas holdup, the overall kLa and the population of the small gas bubbles for N2 in the liquid paraffins mixture were greater than those in the light F-T cut. Operating the SBCR with the heavy F-T cut resulted in the lowest gas holdup and the largest gas bubbles size which led to the lowest gas–liquid interfacial area and consequently, the lowest kLa values. Also, under the operating conditions investigated, the behavior of overall kLa for the gases used in the three F-T cuts in the presence and absence of the three solids employed was controlled by that of the gas–liquid interfacial area (a). Using the data obtained, two novel empirical correlations for predicting the gas holdup and the overall kLa for gases specifically in F-T cuts are proposed.

International Journal of Greenhouse Gas Control, Oct 1, 2022

International Journal of Greenhouse Gas Control, Jul 1, 2022

Fuel Processing Technology, Apr 1, 2008

International Journal of Chemical Reactor Engineering, Aug 30, 2005

The equilibrium gas solubility (C*), gas-holdup (eG), Sauter mean bubble diameter (dS), volumetri... more The equilibrium gas solubility (C*), gas-holdup (eG), Sauter mean bubble diameter (dS), volumetric mass transfer coefficient (kLa), gas-liquid interfacial area (a) and mass transfer coefficient (kL) of N2, O2 and air were measured in an agitated reactor operating in surface-aeration (SAR), gas-inducing (GIR) or gas-sparging (GSR) modes in pure toluene and three mixtures of organic liquids (toluene-benzoic acid-benzaldehyde) aimed at simulating the continuous liquid phase toluene oxidation (LPTO) under wide ranges of temperatures (300-453K), pressures (1-15 bar), mixing speeds (13.3-20.0 Hz), superficial gas velocities (0.000-0.004 m/s in the GSR) and liquid heights (0.171-0.268m in the SAR and GIR). C* values of the gases in the organic liquids were calculated using a modified Peng-Robinson Equation-of-State and kLa data were determined using the Transient Physical Absorption technique. The bubble size distributions as well as dS were obtained from the Photographic method, and eG values were measured through the Dispersion Height technique using the reactor's Jerguson windows. From eG, dS and kLa experimental values, a and kL were calculated under various operating conditions. The Central Composite Statistical Design and analysis technique was used to study the effect of operating conditions on the hydrodynamic and mass transfer parameters. At constant temperature, the equilibrium solubilities (C*) of the three gases in all liquids used appeared to increase linearly with pressure and obey Henry's Law, however, the values exhibited minima with increasing temperature. The C* values

Energy & Fuels, Jul 23, 2021

The chemical engineering journal, Sep 1, 1991

ABSTRACT

Chemical Engineering Science, 1994

Industrial & Engineering Chemistry Research, Feb 11, 2014

The ionic liquid (IL) [hmim][Tf 2 N] was used as a physical solvent in an Aspen Plus simulation, ... more The ionic liquid (IL) [hmim][Tf 2 N] was used as a physical solvent in an Aspen Plus simulation, employing the Peng−Robinson Equation of State (PR-EOS) with Boston−Mathias (BM) α-function and standard mixing rules, to develop a conceptual process for CO 2 capture from a shifted (undergone the water−gas shift reaction) warm fuel gas stream produced from Pittsburgh #8 coal for a 400 MWe IGCC power plant. The physical properties of the IL, including density, viscosity, surface tension, vapor pressure, and heat capacity were obtained from literature and modeled as a function of temperature. Also, available experimental solubility values for CO 2 , H 2 , H 2 S, CO, and CH 4 in this IL were compiled, and their binary interaction parameters (δ ij and l ij) were optimized and correlated as functions of temperature. The Span−Wager EOS was also employed to generate CO 2 solubilities in [hmim][Tf 2 N] at high pressures (up to 10 MPa) and temperatures (up to 510 K). The conceptual process developed consists of four adiabatic absorbers (2.4 m inner diameter (ID), 30 m high) arranged in parallel and packed with Plastic Pall Rings of 0.025 m for CO 2 capture; 3 flash drums arranged in series for solvent (IL) regeneration with the pressureswing option; and a pressure-intercooling system for separating and pumping CO 2 up to 153 bar to the sequestration sites. The compositions of all process streams, CO 2 capture efficiency, and net power were calculated using the Aspen Plus simulator. The results showed that, based on the composition of the inlet gas stream to the absorbers, 95.12 mol % of CO 2 was captured and sent to sequestration sites; 98.37 mol % of H 2 was separated and sent to turbines; and the solvent exhibited a minimum loss of 1.23 mol %. These results indicate that the [hmim][Tf 2 N] IL could be used as a physical solvent for CO 2 capture from warm shifted fuel gas streams with high efficiency.

Aiche Journal, Jul 14, 2015

The main objective of this study is to predict the performance of an industrial-scale (ID 5 5.8 m... more The main objective of this study is to predict the performance of an industrial-scale (ID 5 5.8 m) slurry bubble column reactor (SBCR) operating with iron-based catalyst for Fischer-Tropsch (FT) synthesis, with emphasis on catalyst deactivation. To achieve this objective, a comprehensive reactor model, incorporating the hydrodynamic and mass-transfer parameters (gas holdup, e G , Sauter-mean diameter of gas bubbles, d 32 , and volumetric liquid-side mass-transfer coefficients, k L a), and FT as well as water gas shift reaction kinetics, was developed. The hydrodynamic and mass-transfer parameters for He/N 2 gaseous mixtures, as surrogates for H 2 /CO, were obtained in an actual molten FT reactor wax produced from the same reactor. The data were measured in a pilot-scale (0.29 m) SBCR under different pressures (4-31 bar), temperatures (380-500 K), superficial gas velocities (0.1-0.3 m/s), and iron-based catalyst concentrations (0-45 wt %). The data were modeled and predictive correlations were incorporated into the reactor model. The reactor model was then used to study the effects of catalyst concentration and reactor length-to-diameter ratio (L/D) on the water partial pressure, which is mainly responsible for iron catalyst deactivation, the H 2 and CO conversions and the C 51 product yields. The modeling results of the industrial SBCR investigated in this study showed that (1) the water partial pressure should be maintained under 3 bars to minimize deactivation of the iron-based catalyst used; (2) the catalyst concentration has much more impact on the gas holdup and reactor performance than the reactor height; and (3) the reactor should be operated in the kinetically controlled regime with an L/D of 4.48 and a catalyst concentration of 22 wt % to maximize C 51 products yield, while minimizing the iron catalyst deactivation. Under such conditions, the H 2 and CO conversions were 49.4% and 69.3%, respectively, and the C 51 products yield was 435.6 ton/day.

OSTI OAI (U.S. Department of Energy Office of Scientific and Technical Information), Sep 21, 2022

Social Science Research Network, 2022

Catalysis Today, Jul 1, 2021