Absorption of oxygen by n‐butyraldehyde

Ladhabhoy, M. E.; Sharma, Man Mohan

doi:10.1002/jctb.5010190907

Cited by 10 publications

(2 citation statements)

References 16 publications

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“…Subsequent reaction between the per-acid and the aldehyde gives the final product of the oxidation, the carboxylic acid. From a series of additional experiments, it was found that the reaction has first-order with respect to the oxygen concentration ( n = 1) and second-order with respect to the octanal concentration, which confirms previously published data: r = k r C normalB 2 C normalO 2 where k r = k 0 exp[− E a /( RT )]. The parameters are listed in Table .…”

Section: Reactor Modelsupporting

confidence: 89%

Enhancement of the Liquid-Side Mass Transfer in a Falling Film Catalytic Microreactor by In-Channel Mixing Structures

Rebrov

Duisters

Löb

et al. 2012

Ind. Eng. Chem. Res.

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Catalytic octanal oxidation with oxygen was performed at 100 °C and the total pressure of 5 and 10 bar in a falling film microreactor with varying reaction plates bearing different in-channel mixing structures. The liquid flow rate was changed in the range of 3.3−17.5 mL/min. The liquid-sided mass transfer over grooved or finned structured plates was enhanced by factors of 1.12 and 1.20, respectively, compared to that on a standard plate with 16 microchannels with dimensions of 1200 μm × 400 μm. The liquid flow rate over the structured plates could be increased by 60%−80% without any loss of octanal conversion. A two-dimensional convection and diffusion model adopted from Al-Rawashdeh et al. [Chem. Eng. Sci. 2008, 63, 5149] was formulated to simulate the reactor behavior, and its predictions describe the experimental results in terms of octanal conversion with an accuracy of 4.3% when the actual temperature distribution in the reactor plate is taken into account.

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Section: Reactor Modelsupporting

confidence: 89%

Enhancement of the Liquid-Side Mass Transfer in a Falling Film Catalytic Microreactor by In-Channel Mixing Structures

Rebrov

Duisters

Löb

et al. 2012

Ind. Eng. Chem. Res.

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show abstract

“…The following physical properties of the reaction system butyraldehyde oxidation are used . Diffusion coefficients used are 1.9 × 10 -9 m 2 /s for D O2 and 1 × 10 -9 m 2 /s for D BA .…”

Section: Reaction Model and Experimental Sectionmentioning

confidence: 99%

Reactor Model for Fast Reactions in the Micro-Bubble Column and Validation

Haverkamp

Hessel

Liauw

et al. 2007

Ind. Eng. Chem. Res.

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A simple reactor model for predicting conversions in a micro-bubble column is described. It assumes fast reactions so that the gaseous component is readily consumed at the gas-liquid interface. Then, gas-liquid mass transfer becomes determining. As input parameters for the model, the hydrodynamics, specific interfacial area, and mass transport need to be described. Two fast model reactions, the catalytic oxidation of butyraldehyde and the absorption of CO 2 in aqueous NaOH, show the applicability of the model but also its limits. The model was used for predicting reaction performance in dependence of operating conditions, in particular to get maximum conversion with the antagonistic parameters interfacial area and residence time. The latter cannot be controlled independently when using the reactor engineering principle reported here, but both are triggered by changing the flow rate. The model was then applied to predict reaction performance of the direct fluorination of toluene.

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Backmixing in gas‐liquid reactors

1978

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This review evaluates the present state of the art on backmixing in gas-liquid and gas-liquid-solid reactors. A brief outline of numerous techniques for measuring residence time distribution (RTD) of various phases in a multiphase reactor is presented. This is followed by a brief description of differential and stagewise models for characterizing backmixing from RTD measurements. Both simple (that is, single-parameter axial dispersion model) and more complex (that is, two-, three-, or four-parameter models) models are evaluated. Backmixing characteristics of various gas-liquid columns such as trickle beds, spray columns, mechanically agitated columns, plate columns, fluidized bed columns, etc., are subsequently evaluated. The performance of a bubble column under various reaction conditions is analyzed. Criteria for the elimination of backmixing in packed-bed reactors are presented, and the effect of backmixing on the multiple steady states in a gas-liquid reactor is briefly reviewed. Finally, the scale-up problems associated with gas-liquid reactors with various degrees of backmixing and the recommendations for the future work in RTD and macromixing models are outlined. SCOPEIt is well known that backmixing is detrimental to the performance of a gas-liquid or a gas-liquid-solid reactor. This review outlines various aspects of backmixing in gas-liquid reactors.The review first outlines the methods for measuring residence time distributions for various phases in a gasliquid and a gas-liquid-solid reactor. The data for the residence time distributions (RTD) are evaluated by a variety of simple (for example, one-parameter axial dispersion model) and complex (for example, two-, three-, or four-parameter) differential or stagewise macromixing models. These models are briefly evaluated.From the point of view of backmixing, gay-liquid and gas-liquid-solid reactors can be classified into three broad categories: film reactors where the liquid is the dispersed phase and flows as a film, for example, trickle-bed reactors; gas dispersed as bubbles in a continuous liquid phase, for example, bubble column and slurry reactors; and liquid dispersed as droplets in a continuous gas phase, for example, spray column reactors. Backmixing characteristics of each of these types of reactors are briefly evaluated. The backmixing in these reactors has been largely characterized on the basis of axial dispersion model. Models for gas-liquid bubble column reactors are briefly reviewed. Slow, fast, and instantaneous gas-liquid reactions are considered. Criteria for eliminating the effect of backmixing on the performance of isothermal and adiabatic trickle-bed reactors are outlined. Unlike a singlephase reactor, an adiabatic gas-liquid reactor can lead to five steady states, and the literature on this unique feature of the gas-liquid reactor is briefly reviewed.Finally, there is a brief outline of the scale-up problems associated with RTD, and some recommendations for the future work on RTD and macromixing models are presented. CONCLUSIONS AND...

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Absorption of oxygen by n‐butyraldehyde

Cited by 10 publications

References 16 publications

Enhancement of the Liquid-Side Mass Transfer in a Falling Film Catalytic Microreactor by In-Channel Mixing Structures

Enhancement of the Liquid-Side Mass Transfer in a Falling Film Catalytic Microreactor by In-Channel Mixing Structures

Reactor Model for Fast Reactions in the Micro-Bubble Column and Validation

Backmixing in gas‐liquid reactors

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