Comparison Study of Experimental and Simulation in the Glucose Isomerisation Process in a Fixed-Bed Reactor

2013 ◽  
Vol 781-784 ◽  
pp. 961-964
Author(s):  
N. Abd. Rahman ◽  
Mohd Azlan Hussain ◽  
Jamaliah Md.Jahim
Keyword(s):  
Experimental Data ◽  
Fixed Bed ◽  
Glucose Isomerase ◽  
Fixed Bed Reactor ◽  
Modified Model ◽  
Initial Substrate ◽  
Rate Of Reaction ◽  
Immobilized Glucose Isomerase ◽  
Semi Empirical ◽  
Menten Constant

Production of fructose from glucose isomerisation process using commercial immobilized glucose isomerase (IGI) was conducted in a fixed-bed bioreactor. A semi-empirical kinetic model based on the mechanism of the glucose isomerisation process has been proposed. The values of maximum rate of reaction, Vm ,g L-1 min-1 are (1.82, 1.86, 1.93 and 0.37), for Michaelis-Menten constant Km, g L-1 the values are (1.04, 1.11, 1.24 and 0.35). In this modified model, known as MM3 the variation of temperature, pH, and initial substrate concentration, feed flow rates have been taken into account. The validation of the models with experimental data was checked in terms of AAE and R2. The values of correlation coefficient, R2 (> 0.95) indicated that MM3 model was well fitted to the experimental data.

Evaluation of alkalinity spatial distribution in an up-flow fixed bed anaerobic digester

2017 ◽  
Vol 77 (4) ◽  
pp. 948-959 ◽  
Author(s):  
Maha Hmissi ◽  
Jérôme Harmand ◽  
Victor Alcaraz-Gonzalez ◽  
Hedi Shayeb
Keyword(s):  
Experimental Data ◽  
Experimental Study ◽  
Spatial Distribution ◽  
Volatile Fatty Acids ◽  
Fixed Bed ◽  
Control Process ◽  
Fixed Bed Reactor ◽  
Hydrodynamic Behavior ◽  
Sampling Points ◽  
Tequila Vinasses

Abstract In this paper, an experimental study upon alkalinity and hydrodynamic behavior in an anaerobic up-flow fixed bed reactor for the treatment of tequila vinasses is presented. Measurements of volatile fatty acids, pH, alkalinity and bicarbonate were obtained at three sampling points in the reactor in the axial axis. Then, the spatial distribution of alkalinity is studied and discussed. Moreover, for further control process purposes, a hydrodynamic model based on the use of two interconnected two-steps reduced AM2 type models is proposed and its parameters are identified using experimental data.

scholarly journals Synthesis of methanol in microchnnel

2021 ◽  
Vol 2119 (1) ◽  
pp. 012113
Author(s):  
S V Dimov
Keyword(s):  
Experimental Data ◽  
Carbon Monoxide ◽  
Chemical Reactions ◽  
Synthesis Gas ◽  
Methanol Synthesis ◽  
Fixed Bed ◽  
Fixed Bed Reactor ◽  
Microchannel Reactor ◽  
Flow Rates ◽  
Synthesis Of Methanol

Abstract Systematic experimental data have been obtained on the results of catalytic chemical reactions in a microchannel reactor for the synthesis of methanol from synthesis gas. Synthesis gas contains hydrogen, carbon monoxide and dioxide, as well as nitrogen in the ratio 58/29/5/8. The experiments were carried out at different flow rates in the temperature range 190-260C. Experiments were also carried out for methanol synthesis in fixed bed reactor at different synthesis pressures.

Simulation Analysis of Fixed Bed Reactor for Au-Cu Non-Mercury Catalytic Acetylene Hydrochlorination

2013 ◽  
Vol 455 ◽  
pp. 94-98 ◽  
Author(s):  
Lei Wang ◽  
Ben Xian Shen ◽  
Ruo Fan Ren ◽  
Ji Gang Zhao
Keyword(s):  
Experimental Data ◽  
Simulation Analysis ◽  
Hot Spot ◽  
Fixed Bed ◽  
Axial Direction ◽  
Fixed Bed Reactor ◽  
Two Dimensional ◽  
Acetylene Hydrochlorination ◽  
Valuable Data ◽  
Operation Conditions

A two-dimensional pseudo-homogenous mathematical model was established according to the Au-Cu non-mercury catalytic reaction kinetics. The Crank-Nicholson method was used to solve the equations on the basis of experimental data. The results showed that a violent reaction at the entrance of the fixed bed reactor led to a hot spot in the acetylene hydrochlorination reaction over the Au-Cu Non-mercury catalyst. The conversion increased rapidly initially, and then flattened gradually in the axial direction. The result of simulation provided valuable data to optimize the design of reactor and the industrial operation conditions.

Hydrogenation of Acetylene: Kinetic Studies and Reactor Modeling

2005 ◽  
Vol 3 (1) ◽  
Author(s):  
Navid Mostoufi ◽  
Ali Ghoorchian ◽  
Rahmat Sotudeh-Gharebagh
Keyword(s):  
Experimental Data ◽  
Catalyst Deactivation ◽  
Fixed Bed ◽  
Kinetic Studies ◽  
Operating Conditions ◽  
Fixed Bed Reactor ◽  
Reactor Modeling ◽  
Deactivation Rate Constant ◽  
Hydrogenation Reactor ◽  
Kinetics Of

The kinetics of acetylene hydrogenation has been studied in a fixed bed reactor of a commercial Pd/Al2O3 catalyst. The experiments were carried out at 30, 50 and 70 ºC with various feed compositions at atmospheric pressure. The experiments were repeated at 70 ºC in the presence of the used catalyst to determine the effect of the catalyst deactivation where the corresponding deactivation rate constant was determined in order to predict the activity of the catalyst during each run. Two well known kinetic models were used for a nearly similar catalyst to predict the experimental data of this work and none of them were found satisfactory. A new model was then proposed to fit the experimental data. The hydrogenation reactor was also simulated at industrial operating conditions with the proposed kinetics for both plug and dispersion flows. The results of these simulations were almost close to each other in most cases.

A Study of High-Pressure CO2 Recycling Using Pinewood Char Gasification

2013 ◽  
Author(s):  
Indraneel Sircar ◽  
Anup Sane ◽  
Jay Gore
Keyword(s):  
Experimental Data ◽  
Mass Loss ◽  
Large Scale ◽  
High Pressures ◽  
Fixed Bed ◽  
High Sensitivity ◽  
Reaction Rates ◽  
Fixed Bed Reactor ◽  
Loss Data ◽  
High Pressure Co2

Measurements of the reaction rates at high-pressures for gasification of low-ash pinewood char with CO2 are presented. A fixed-bed reactor operated at 1140–1260 K and 1–10 atm was utilized in the present study. Product gas sampling and gas chromatograph measurements enabled tracking of the gasification progress and mass loss data. The mass loss data are interpreted using the volumetric and non-reactive core models. Activation energy, collision frequency and reaction order are reported for each model. The experimental data show high sensitivity to temperature. The data also show an increase of the apparent gasification rates with higher CO2 pressures. Comparison of computed char conversion profiles and experimental data are discussed in the context of mass transport and effects on the gasification rates. The findings from this study have applications to gasification modeling and design of large-scale gasification systems.

Development of a Kinetic Model for Modeling the Industrial VGO Hydrocracker Accompanied By Deactivation

2010 ◽  
Vol 8 (1) ◽  
Author(s):  
Azita Barkhordari ◽  
Shohreh Fatemi ◽  
Mahdi Daneshpayeh ◽  
Hossain Zamani
Keyword(s):  
Experimental Data ◽  
Kinetic Model ◽  
Catalyst Deactivation ◽  
Fixed Bed ◽  
Pilot Scale ◽  
Operating Conditions ◽  
Fixed Bed Reactor ◽  
Wide Range ◽  
Silica Alumina ◽  
Parallel Reactions

Two types of kinetic modeling, continuous and discrete lump model were studied and compared in this research in order to model the industrial scale VGO hydrocracking process. The experimental data obtained from a pilot-scale fixed bed reactor over Ni-Mo/Silica-Alumina catalyst in a wide range of operating conditions was used for prediction and tuning the kinetic parameters using Genetic algorithm. In this study, the discrete lump model with four parallel reactions to four lumped products showed more convergence to the experimental data than the continuous lump model. Afterward, the discrete kinetic model was used to simulate the vacuum gas oil (VGO) industrial hydrocracking reaction accompanied by catalyst deactivation. The activity of the catalyst was taken as a time dependent variable and the first year of operational data were used to derive the deactivation parameter. The refinery test runs spanning over the last two and half years of operation were used to validate the model and interpret the simulation results. A comparison between the industrial and the predicted data showed that there is a good agreement between them and the presented model provides a reasonable fit to estimate the product yields of LPG, naphtha, kerosene, diesel.

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