Multitubular reactor design as an advanced screening tool for three-phase catalytic reactions

Mäki‐Arvela, Päivi; Eränen, Kari; Alho, Kasper; Salmi, Tapio; Murzin, Dmitry Yu.

doi:10.1007/s11244-007-0270-3

Cited by 8 publications

(7 citation statements)

References 6 publications

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“…Furthermore, six TBRs in parallel were used to intensify generation of the experimental data. 1 When deactivation in a batch reactor is compared to that in a…”

Section: Discussionmentioning

confidence: 99%

“…Experimental kinetic data were obtained using six reactors in parallel. 1 This modeling study concentrates on the first reaction step in the straight synthesis of menthol, the hydrogenation of citral to citronellal. Experimental data from citral hydrogenation was used for model testing and fine-tuning.…”

Section: Introductionmentioning

confidence: 99%

“…The experimental study was carried out in a new packed-bed reactor system, designed in our laboratory (Figure ). Experimental kinetic data were obtained using six reactors in parallel . This modeling study concentrates on the first reaction step in the straight synthesis of menthol, the hydrogenation of citral to citronellal.…”

Section: Introductionmentioning

confidence: 99%

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Modeling of a Three-Phase Continuously Operating Isothermal Packed-Bed Reactor: Kinetics, Mass-Transfer, and Dispersion Effects in the Hydrogenation of Citral

Kilpiö

Mäki‐Arvela

Rönnholm

et al. 2011

Ind. Eng. Chem. Res.

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A continuously operating isothermal dynamic packed-bed reactor was modeled. The model included chemical reaction, gas–liquid mass transfer, convection, axial dispersion, pore diffusion, and catalyst deactivation. The model was solved by using the method of lines. The model was applied on experimental data from citral hydrogenation over a supported nickel catalyst. The experiments had been carried out at 25–65 °C and at 6.1 bar in a laboratory-scale trickle-bed reactor (d = 1 cm; L = 5 cm). The parameters in the model were the rate constants, pore diffusivity, coking rate constant, Peclet number, and gas–liquid mass-transfer coefficient. A sensitivity study was performed to reveal how much a change in each of these changed the product concentration trend. The simulations revealed that the gas–liquid mass-transfer coefficient and effective diffusivity should have been well below expected values to significantly reduce the productivity. The gas–liquid mass transfer and pore diffusion were not rate-limiting; because hydrogen was used in excess, particles were small and the system was dilute. The citral concentration-dependent deactivation model based on site competition was able to describe the observed activity decline. Parameter estimation for the reaction rate and coking rate was carried out. A reasonable agreement with the experimental trends was obtained. An estimate of the Peclet number was obtained from step-response measurements with an inert tracer, which revealed that the reactor did not operate completely as a plug-flow unit. The model described here can be extended to be applicable for other hydrogenation and oxygenation reactions of other fine chemicals.

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“…Furthermore, six TBRs in parallel were used to intensify generation of the experimental data. 1 When deactivation in a batch reactor is compared to that in a…”

Section: Discussionmentioning

confidence: 99%

Section: Introductionmentioning

confidence: 99%

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Modeling of a Three-Phase Continuously Operating Isothermal Packed-Bed Reactor: Kinetics, Mass-Transfer, and Dispersion Effects in the Hydrogenation of Citral

Kilpiö

Mäki‐Arvela

Rönnholm

et al. 2011

Ind. Eng. Chem. Res.

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“…A reactor setup of six‐parallel tube reactors (constructed in stainless steel 316 L) was used for the continuous hydrogenation . The inner diameter of the reactor tubes was 10 mm, and the catalyst was placed into the reactor by using glass wool and metal nets as supports for the catalyst bed.…”

Section: Methodsmentioning

confidence: 99%

The Impact of Salts Formed by the Neutralisation of (Ligno)Cellulose Hydrolysates on the Hydrogenation of Sugars

et al. 2018

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Dilute acid hydrolysis of lignocellulose often requires a neutralisation step to utilise the hydrolysate's sugars. In this context, very little is known regarding the impact of low levels of acids or their corresponding salts produced by neutralisation on the catalyst performance in the hydrogenation of sugars. In this work, the influence of a series of ammonium and alkali metal salts (that is, NH4NO3, NaNO3, (NH4)2SO4, Na2SO4 and K2SO4) on the hydrogenation of glucose and xylose is addressed. This study also encompasses “real‐world” hydrolysates obtained by the mechanocatalytic depolymerisation of α‐cellulose and beechwood. The impact of low levels of acids and their salts upon the hydrogenation of sugars to sugar alcohols (alditols) was examined, in the presence of a commercial Ru/C catalyst (Ru/C, 0.7 wt % Ru) at 110 °C using batch and trickle‐bed reactors. The results show that the presence of salts leads to a considerable decrease in the alditols yields. Notably, salt anions exert an effect stronger than that of cations in the catalyst deactivation. Surprisingly, nitrates had a more significant effect on the decrease in the alditols yield than sulfates, and chlorides had the lowest impact. In this study, we also present the effect of sugars’ degradation products (e.g. 5‐(hydroxymethyl)furfural and furfural) upon hydrogenation of lignocellulose hydrolysates. The activated carbon pre‐treatments of the hydrolysates showed a positive effect on the catalyst activity, adsorbing hydrolysis by‐products. Overall, this study has significant implications for the practical aspects of hydrogenation of lignocellulose hydrolysates, which are often neglected in the current literature.

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“…More recently a significant decrease in conversion [11] from 40 to 20% within 40 min time-on-stream was obtained in liquid phase citral hydrogenation in ethanol over a fixed bed of Ni/SiO 2 catalyst operating already at 25 • C, and 6.1 bar total pressure, clearly demonstrating significant deactivation.…”

Section: Qualitative Kineticsmentioning

confidence: 98%

Enhancing consecutive reactions during three phase hydrogenation with a semibatch liquid phase

Mäki‐Arvela

Denecheau

Alho

et al. 2007

Chemical Engineering Journal

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Multitubular reactor design as an advanced screening tool for three-phase catalytic reactions

Cited by 8 publications

References 6 publications

Modeling of a Three-Phase Continuously Operating Isothermal Packed-Bed Reactor: Kinetics, Mass-Transfer, and Dispersion Effects in the Hydrogenation of Citral

Modeling of a Three-Phase Continuously Operating Isothermal Packed-Bed Reactor: Kinetics, Mass-Transfer, and Dispersion Effects in the Hydrogenation of Citral

The Impact of Salts Formed by the Neutralisation of (Ligno)Cellulose Hydrolysates on the Hydrogenation of Sugars

Enhancing consecutive reactions during three phase hydrogenation with a semibatch liquid phase

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