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Mathematical model involving chemical reaction and mass transfer for the ozonation of dimethyl phthalate in water in a bubble column reactor

  • Jianbing Wang EMAIL logo , Zhilin Xia , Zuhai Cao , Shaoxia Yang and Wanpeng Zhu
Published/Copyright: February 7, 2017
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Abstract

This research investigated the establishment of a mathematical model for the ozonation of dimethyl phthalate (DMP) through the analysis of the mass transfer and reactions in a semi-batch bubble column reactor. Negative step tracer experiments were conducted with ozone as a tracer, which indicated that the gas phase is perfectly well mixed at the gas flow rate of 400 mL/min. Based on the results from ozone absorption experiments the mass transfer coefficient of ozone was determined to be 0.0054 s−1. The measured stoichiometry ratio of the direct reaction between ozone and DMP was about 5. The calculated rate constant was 0.87 L/(mol·s) for the direct reaction between ozone and DMP. A mathematical model was established based on the component mass balance in the reaction system involving the direct and indirect reactions and mass transfer between gas and liquid phases enhanced by the chemical reactions. The model can predict the removal of DMP for the early stage of the ozonation process well. At the latter stage, the predicated removals deviated from the measured results mainly due to the consumption of ozone by side reactions.

Acknowledgements

Thanks are given to the National Natural Science Foundation of China (Project No. 20907072) for the financial support of this work.

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Nomenclature

CDMPConcentration of DMP in liquid phase
CDMP,0Initial concentration of DMP in liquid phase
CHOConcentration of HO· in liquid phase
CO3IInterfacial concentration of ozone in the gas-liquid film (mol/L)
CO3GConcentration of ozone in gas phase (mol/L)
CO3GGas-phase concentration of ozone at the reactor inlet (mol/L)
CO3LConcentration of ozone in aqueous phase
CO3(t)Concentration of tracer (ozone) at time t
CO30Concentration of tracer (ozone) at initial time
CPiConcentrations of the products in liquid phase
CTBAConcentrations of the scavengers in liquid phase
DTDiameter of the bubble column (m)
DDMPDiffusion coefficient of DMP in water (cm2/s)
DO3Diffusion coefficient of ozone in water(cm2/s)
EEnhancement factor
E(t)Residence time distribution function, E(t)=dF(t)dt
F(t)Evolution of dimensionless tracer (ozone) concentration,F(t)=CO3t/CO30
HTHeight of liquid in the bubble column with aeration (m)
H0Height of liquid in the bubble column without aeration (m)
NNumber of tanks in series
NO3LMolar flux of ozone diffusing from the outer edge of a liquid element (film) to the main liquid (M/(m2·s))
NO30Molar flux of ozone diffusing from the gas into the interface (M/(m2·s))
QGas flow rate (m3/s)
SROzone solubility rate
TTemperature of the solution (K)
VDMPMolar volume of DMP in the solution, 214.6 cm3/mol
aSpecific interfacial area between gas and liquid phases (m2/m3)
kDMPHO.Rate constant for the reaction between DMP and hydroxyl radical
kLChemical mass transfer coefficient of ozone (m/s)
kLaVolumetric mass transfer coefficient of ozone in water (s−1)
kL0Physical mass transfer coefficient of ozone (m/s)
kO3DMPSecond-order rate constant for the reaction between ozone and DMP (L/(mol·s))
kPiRate constant for the reaction between the products and hydroxyl radical
kTBARate constant for the reaction between the scavengers and hydroxyl radical
kdFirst-order rate constant for the self-decomposition of ozone (s−1)
k1Rate constant for the reaction between O3 and OH, 70 M−1S−1
rStoichiometry of the reaction between ozone and DMP
tTime (s)
tmMean residence time of the actual distribution function (s), tm=0tE(t)dt
ugSuperficial gas velocity (m/s), ug=4QπDT2
βGas holdup, β=HTH0HT
ηRatio of molar fluxes of ozone
μViscosity of water (Pa·s)
σVariance of distribution, σ2=0(tτ)2E(t)dt
τiHydraulic residence time of the ith tank (s)
Received: 2016-1-11
Revised: 2016-7-26
Accepted: 2016-9-22
Published Online: 2017-2-7
Published in Print: 2017-1-1

© 2017 by Walter De Gruyter GmbH

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