scholarly journals Determination and Application of Improved Kinetic Parameters for Simulation of Maleic Anhydride Synthesis in Industrial Fixed- Bed Reactor

2019 ◽  
Vol 11 (1) ◽  
Author(s):  
Ervin Karić ◽  
Ivan Petric ◽  
Vladan Mićić
Keyword(s):  
Kinetic Model ◽  
Kinetic Parameters ◽  
Kinetic Models ◽  
Fixed Bed ◽  
Fixed Bed Reactor ◽  
Inlet Concentration ◽  
Reactor Performance ◽  
Outlet Concentration ◽  
Reactor Kinetic ◽  
In Series

The aims of this study were to determine improved kineticparameters in five kinetic models for oxidation of n-butane intomaleic anhydride in an industrial fixed-bed reactor, and tosimulate the reactor performance. On the basis of the measuredprocess parameters, inlet and outlet concentrations of n-butanewere calculated and then used to fit the kinetic models. Theindustrial fixed-bed reactor was approximated by 10 continuousstirred tank reactors (CSTR) connected in series. Based on thecalculated outlet concentration of n-butane from the industrialreactor, the outlet concentration of n-butane from thepenultimate reactor was calculated. Then the concentrations ofn-butane were calculated until the inlet concentration of nbutanein the first reactor was obtained. Kinetic parameterswere determined by comparing the inlet concentrations of nbutanein the first reactor with the inlet concentration of nbutaneobtained on the basis of the measured processparameters in the industrial fixed-bed reactor. Kinetic modelswith improved kinetic parameters showed better simulationresults compared to kinetic models with the existing kineticparameters. The best agreement of simulation results andmeasured values was achieved with application of the kineticmodel 2 (Equations (2a-c)). The smallest deviations ofnumerical simulation in comparison with measured values of theoutlet pressure of reaction mixture were 0.45, 0.75 and 0.75%for application of the kinetic model 3 (Equations (3a-c)). Thepercentage deviations of numerical simulation with improvedkinetic parameters and the existing kinetic parameters incomparison with measured values of inside reactor temperaturewere in the range 0.90-5.36% and in the range 4.17-9.78%(kinetic model 2, Equations (2a-c)), respectively.

Pyrolysis Characteristics and Kinetics of Cassava Residues

2014 ◽  
Vol 953-954 ◽  
pp. 325-329
Author(s):  
Jin Wei Jia ◽  
Di Yang ◽  
He Long Hui ◽  
Xing Min Fu ◽  
Lu Liu ◽  
...  
Keyword(s):  
Activation Energy ◽  
Kinetic Parameters ◽  
Fixed Bed ◽  
The Other ◽  
Fixed Bed Reactor ◽  
Biomass Feedstock ◽  
Pyrolysis Characteristics ◽  
Three Samples ◽  
Bio Oil ◽  
Kinetics Of

The aims of this work were to investigate the influence of feedstock properties of different part of cassava residues (cassava rhizome (CR), cassava stalk (CS) and cassava leaf (CL)) and operating temperatures on the pyrolysis characteristics and the kinetic parameters. Pyrolysis experiments of three selected biomass feedstock were conducted using a fixed-bed reactor. It was shown that the bio-oil yield of cassava stalk reached the maxima at 600°C, and the char yield reduced with the temperature, whereas the gas yield increased with temperature. The cassava rhizome presented higher thermochemical reactivity than the other samples. The activation energy of cassava stalks was 37.57 kJ / mol and that of cassava rhizome (39.42 kJ / mol) increased slightly. The activation energy of cassava leaf (22.85 kJ / mol) was lowest of the three samples.

Activity and selectivity of non-uniform bifunctional catalysts. Analysis of the fixed-bed reactor performance

1986 ◽  
Vol 51 (11) ◽  
pp. 2509-2520 ◽  
Author(s):  
Darío R. Ardiles
Keyword(s):  
Fixed Bed ◽  
Product Distribution ◽  
Bifunctional Catalyst ◽  
Fixed Bed Reactor ◽  
Bifunctional Catalysts ◽  
Reactor Performance ◽  
Catalytic Functions ◽  
Reaction Schemes

This paper reports a study about the effect of activity distributions of a bifunctional catalyst on the conversion and product distribution in a fixed-bed reactor. Uniform as well as increasing and decreasing activity profiles of both catalytic functions are considered. The analysis is performed assuming three different reaction schemes. Results show that reactor performance is greatly affected by the use of catalysts with non-uniform activity distributions.

Optimal catalyst activity distribution in fixed-bed reactor with catalyst deactivation

1989 ◽  
Vol 54 (2) ◽  
pp. 375-387 ◽  
Author(s):  
Jozef Markoš ◽  
Alena Brunovská
Keyword(s):  
Catalyst Deactivation ◽  
Active Catalyst ◽  
Catalyst Activity ◽  
Fixed Bed ◽  
Fixed Bed Reactor ◽  
Catalytic Reactor ◽  
Reactor Performance ◽  
Thiele Modulus ◽  
Activity Distribution ◽  
Parameter Ratio

In this paper the influence of the active catalyst location in a pellet on fixed-bed catalytic reactor performance is described. The optimal activity distribution as a function of an economic parameter (ratio of product and catalyst costs), Thiele modulus and Damkohler number is estimated.

scholarly journals A Useful Excel-Based Program for Kinetic Model Discrimination

2018 ◽  
Vol 2 (4) ◽  
pp. 57 ◽  
Author(s):  
Lidia Pino ◽  
Vincenzo Recupero ◽  
Agustín Hernández
Keyword(s):  
Regression Analysis ◽  
Kinetic Model ◽  
Linear Regression ◽  
Kinetic Parameters ◽  
Kinetic Models ◽  
Linear Regression Analysis ◽  
Dry Reforming ◽  
Model Discrimination ◽  
Enzyme Kinetic ◽  
User Friendly

In the present study, the ANEMONA.XLT tool, an Excel template that was designed for calculation of enzyme kinetic parameters, has been successful adapted to some proposed models for dry reforming reaction, such as Eley-Rideal or Langmuir-Hinshelwood kinetic models. Model discrimination by non-linear regression analysis has been applied to data from the literature; the predicted kinetic parameters that were obtained using ANEMONA.XLT were fully comparable with those already published. Thus, the template can be a helpful and user-friendly alternative tool for researchers who do not have advanced skills in computer programming.

scholarly journals Kinetic Model of Crude Palm Oil Hydrocracking Over Ni/Mo ZrO2–Pillared Bentonite Catalyst

2019 ◽  
Vol 64 (2) ◽  
pp. 238-247 ◽  
Author(s):  
Hasanudin Hasanudin ◽  
Addy Rachmat ◽  
Muhammad Said ◽  
Karna Wijaya
Keyword(s):  
Kinetic Model ◽  
Palm Oil ◽  
Rate Constants ◽  
Catalyst Activity ◽  
Fixed Bed ◽  
Diesel Oil ◽  
Fixed Bed Reactor ◽  
Crude Palm Oil ◽  
Reaction Models ◽  
Oil Gas

Crude Palm Oil hydrocrcaking has been carried out over Ni/Mo ZrO2–pillared bentonite catalyst in a fixed bed reactor. Crude Palm Oil hydrocracking over Ni/Mo ZrO2–pillared bentonite catalyst formed 3 products i.e. gas, oil and coke. The oil product from Crude Palm Oil hydrocracking was analyzed by using gas chromatography to determine its composition. Three types of fraction were classified i.e. gasoline, kerosene and diesel oil. In this research, the focused of the study is of hydrocracking kinetics by using lump kinetic models. The kinetic model was solved by using the software MATLAB R2018b involves the effect of catalyst activity on the reaction rate. The results of the kinetic study show that the 4-lump (Crude Palm Oil, gas coke and oil) and 6-lump reaction models (Crude Palm Oil, gas, coke, gasoline, kerosene and diesel) can be used to explain the Crude Palm Oil hydrocracking over Ni/Mo ZrO2–pillared bentonite catalyst. The 4-lump kinetic model has 5 rate constants and the 6-lump kinetic model has 14 rate constants.

Kinetics of Camphene Esterification to Isobornyl Acetate

2011 ◽  
Vol 233-235 ◽  
pp. 990-998 ◽  
Author(s):  
Dian Hua Liu ◽  
Ding Ye Fang ◽  
Qin Qin Guan ◽  
A Jian Tao
Keyword(s):  
Acetic Acid ◽  
Kinetic Model ◽  
Continuous Process ◽  
Fixed Bed ◽  
Space Velocity ◽  
Batch Process ◽  
Fixed Bed Reactor ◽  
Feed Ratio ◽  
Continuous Reaction ◽  
Kinetics Of

The conventional process for isobornyl acetate synthesis from camphene and acetic acid is a batch process. The purpose of this paper is to synthesize isobornyl acetate in continuous process in a fixed bed reactor. The continuous reaction conditions were studied. The experiment was put into practice under the following conditions: 35-45, camphene/acetic acid feed ratio(wt%) from 1 to 2 and space velocity from 0.6 to 1.8 h-1. A kinetic model was developed which describes the experimental data well. A pilot fixed reactor was simulated by using the kinetic model.

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