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

Papers by Badie I. Morsi

Modeling and simulation of a commercial-scale slurry bubble column rector for Fischer-Tropsch synthesis

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

Il est facile d'écrire la transformation de LORENTZ, dans le cas général, sous forme matricielle,... more Il est facile d'écrire la transformation de LORENTZ, dans le cas général, sous forme matricielle, ce qui permet de respecter l'indissociabilité du temps et de l'espace. L'intérêt de cette représentation est de pouvoir démontrer aisément divers aspects de la relativité restreinte, comme la composition des vitesses, la rotation de THOMAS-WIGNER, la transformation de sommes de forces et de couples. Le cas du paradoxe des jumeaux est également abordé.

Coal-Agglomeration Processes: A Review

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.

Hydrodynamic and Mass Transfer Characteristics in a Large-Scale Slurry Bubble Column Reactor for Gas Mixtures in Actual Fischer–Tropsch Cuts

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.

Development of an innovative process for post-combustion CO2 capture to produce high-value NaHCO3 nanomaterials

International Journal of Greenhouse Gas Control, Oct 1, 2022

Unique nanotechnology converts carbon dioxide to valuable products

Physical solvents and techno-economic analysis for pre-combustion CO2 capture: A review

International Journal of Greenhouse Gas Control, Jul 1, 2022

Fuel Processing Technology, Apr 1, 2008

A large number of experimental data points (7374) obtained in our laboratory as well as from the ... more A large number of experimental data points (7374) obtained in our laboratory as well as from the literature, covering wide ranges of reactor geometry (reactor diameter and type, impeller diameter and gas distribution scheme), physicochemical properties (liquid and gas density and molecular weight, liquid viscosity and surface tension, diffusivity) and operating variables (superficial gas velocity, temperature, pressure, mixing speed, liquid height and mixtures) were used to develop empirical as well as back-propagation neural network (BPNN) correlations in order to predict the hydrodynamic and mass transfer parameters in gas-liquid agitated reactors (ARs). The empirical and BPNN correlations developed were incorporated in a calculation algorithm for predicting the gas holdup (ε G ), volumetric mass transfer coefficients (k L a), Sauter mean bubble diameter (d S ), gas-liquid interfacial area (a) and liquid-side mass transfer coefficient (k L ) in ARs, operating in surface-aeration, gas-inducing and gas-sparging modes. The algorithm was used to predict the effects of liquid viscosity and hydrogen mole fraction in the feed gas (H 2 + N 2 ) on the hydrodynamic and mass transfer parameters for the soybean oil hydrogenation process conducted in a large-scale gas-sparging agitated reactor (7000 kg soybean oil capacity). The predictions showed that increasing the liquid-phase viscosity, mimicking the evolution of the hydrogenation of soybean oil in a batch reactor, decreased ε G and increased d S , resulting in a decrease of a. The decrease of the gas holdup with increasing the liquid-phase viscosity was related to the increase of gas bubble coalescence in the reactor. Increasing liquid-phase viscosity, however, decreased k L as well as k L a values for both H 2 and N 2 within the range H 2 mole fraction (0-1) used. This k L behavior indicated that the effect of viscosity on k L is more significant than that of d S , since k L was reported to be proportional to d S . The predictions also showed that increasing the H 2 mole fraction in the feed to the reactor decreased ε G and increased d S , resulting in a decrease of a and an increase of k L as well as k L a for both H 2 and N 2 within the range of liquid-phase viscosity used (0.0023-0.0047 Pa s). The decrease of the gas holdup with increasing the H 2 mole fraction in the feed gas was attributed to the decrease of the density (momentum) of the gas mixture. The increase of k L values with increasing the H 2 mole fraction in the feed gas was related to the increase of d S . The predicted k L a values indicated that the mass transfer behavior in the large-scale gas-sparging reactor proposed for soybean oil hydrogenation was controlled by the mass transfer coefficient, k L . Also, under similar conditions, k L a values for H 2 in soybean oil when using the gaseous mixture (H 2 + N 2 ) were lower than those obtained for H 2 (as a single-component); and k L values for H 2 were consistently greater than those of N 2 within the ranges of the operating conditions used in the simulation.

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

Carbon Dioxide Conversion to Nanomaterials: Methods, Applications, and Challenges

Energy & Fuels, Jul 23, 2021

Mass transfer characteristics of gases in n-decane at elevated pressures and temperatures in agitated reactors

The chemical engineering journal, Sep 1, 1991

ABSTRACT

Chemical Engineering Science, 1994

-The solubility, C*, and volumetric mass transfer cxxficient, k,o, values for hydrogen and ethyle... more -The solubility, C*, and volumetric mass transfer cxxficient, k,o, values for hydrogen and ethylene in liquid propylene were obtained in a 41 surface-aeration agitated reactor operating under pressures between 11 and 55 bar, temperatures from 297 to 333 K, and mixing speeds of 13.3-20.0 Hz. The pressuretime profile of the hydrogen-propylene system exhibited an anomalous behavior due to the vaporization of liquid propylene into the gas phase. The equilibrium gas solubilities were calculated using a modified Peng-Robinson equation of state (PREOS) and the mass transfer coefficients were determined using the transient physical gas absorption technique. A calculation procedure for determining the equilibrium composition and mass transfer coefficients for hydrogen in liquid propylene which accounted for the anomalous behavior of this system was developed. The equilibrium vapor-liquid mole fractions obtained using this procedure compared favorably with available literature values. The C* values were found to increase with the partial pressure of the solute gas. The kLa values increased with mixing speed for both gases, The solubilities of ethylene in liquid propylene were found to be higher than those of hydrogen, whereas the mass transfer coefficients for hydrogen were appreciably higher than those of ethylene. An empirical correlation which predicted k,a values for hydrogen and ethylene gases in liquid propylene in a surface-aeration reactor with an accuracy of + 30% was developed.

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.

Review of Techno-Economic Analysis Studies Using Physical Solvents for Pre-Combustion CO2 Capture

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

Performance of Hydrophobic Physical Solvents for Pre-Combustion Co2 Capture at a Pilot Scale Coal Gasification Facility

Social Science Research Network, 2022

Catalysis Today, Jul 1, 2021

The aim of this study is to perform a techno-economic assessment of the Fischer-Tropsch synthesis... more The aim of this study is to perform a techno-economic assessment of the Fischer-Tropsch synthesis (FTS) process in a microchannel reactor (MCR) to produce clean syncrude, and the Direct Methane to Methanol (DMTM) process in a compact plant footprint. The operational and economic performances of the two processes were modeled using the Aspen HYSYS v7.2. The operational performance parameters include products yield and the economic performance parameters include net present value (NPV), payback period (PBP) and internal rate of return (IRR). In addition, the effects of tailgas recycle ratios and water integration on the performances of the FTS process and the effect of methane recycle ratios on the performances of the DMTM were investigated. The simulation results showed that the unit cost of the DMTM process was sensitive to the methane recycle ratio, however, that of the FTS in MCR was less sensitive to the tailgas recycle ratios. In order to maintain an IRR > 10 %, the tail gas recycle ratio of the FTS in MCR had to be greater than 8 % and 30 %, at CO conversions of 80 % and 72 %, respectively, whereas in the DMTM process, a minimum methane recycle ratio of 60 % was required to achieve any profitability. In addition, the DMTM process appeared to have significantly higher net energy requirements per product yield when compared with those of the FTS in MCR process; however, both processes had higher energy requirements than those of conventional GTL technologies. The FTS synthesis provides a pathway for converting carbon-containing feedstocks, such as natural gas, coal, heavy residue, biomass, municipal waste, etc., into a syngas (CO and H 2 ). After cleaning and conditioning, the CO and H 2 react in the presence of a catalyst,

Performance of hydrophobic physical solvents for pre-combustion CO2 capture at a pilot scale coal gasification facility

International Journal of Greenhouse Gas Control