Design of a two-stage fluidized bed reactor for preparation of diethyl oxalate from carbon monoxide

Jiang, Chongwen; Zheng, Zu-Wei; Zhu, Yaping; Luo, Zheng‐Hong

doi:10.1016/j.cherd.2011.10.018

Cited by 14 publications

(4 citation statements)

References 38 publications

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“…To validate the efficiency and accuracy of the iterative method for the multiscale simulation, we selected the lower part of a two-dimensional (2D) two-stage FBR (TS-FBR), which was reported in our previous works, , as the simulated reactor (see Figure ). In addition, the model parameters and boundary conditions were listed in Tables 1 and 2 of the Supporting Information. ,,, Unless otherwise noted, the parameters used for the forthcoming simulations are those in SI Tables 1 and 2.…”

Section: Simulation Conditions and Modeling Methodsmentioning

confidence: 99%

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Iterative Multiscale Computational Fluid Dynamics–Single-Particle Model for Intraparticle Transfer and Catalytic Hydrogenation Reaction of Dimethyl Oxalate in a Fluidized-Bed Reactor

Zhu

Chen

Luo

et al. 2013

Ind. Eng. Chem. Res.

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In this work, the coupled model based on an iterative approach was developed to describe the flow behavior and catalytic hydrogenation of dimethyl oxalate (DMO) in a fluidized-bed reactor (FBR). First, a single-particle model (SPM) and a computational fluid dynamics (CFD) model were constructed, respectively. A set of hyperbola-like kinetics equations were included in the SPM. Subsequently, we assumed that all catalyst particles inside each small computational cell for the CFD model experience the same external conditions, which ensures the effective coupling of the two models above. The assumption and the coupled model have been validated by evaluating the above assumption and comparing with the experimental data, respectively. Based on the validated model, the predictions of the two classical diffusion equations (i.e., the Wilke−Bosanquet diffusion equation and the Fick or Wilke diffusion equation) are compared. In addition, the main flow field and reaction parameters in the FBR were investigated numerically. The results indicated that the intrapartice transfer resistance rises with the increase of the particle size, while it is not obvious for the selected studied system. The results also indicated that all of the species mass fraction distributions become more even as the catalyst size becomes smaller and the different diffusion models have little influence on simulation results. The simulated results here also demonstrated that one is capable of investigating reactor behavior at relatively low computational cost by using the proposed multiscale model.

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Section: Simulation Conditions and Modeling Methodsmentioning

confidence: 99%

“…In addition, the model parameters and boundary conditions were listed in Tables 1 and 2 of the Supporting Information. 5,67,73,78 Unless otherwise noted, the parameters used for the forthcoming simulations are those in SI Tables 1 and 2.…”

Section: Simulation Conditions and Modeling Methodsmentioning

confidence: 99%

Iterative Multiscale Computational Fluid Dynamics–Single-Particle Model for Intraparticle Transfer and Catalytic Hydrogenation Reaction of Dimethyl Oxalate in a Fluidized-Bed Reactor

Zhu

Chen

Luo

et al. 2013

Ind. Eng. Chem. Res.

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“…Comparison of typical pyrolysis processes suggested that a multistage fluidized bed process had its own advantages in treating coal powder to produce high‐quality tar and syngas and in capturing carbon dioxide with a temperature swing adsorption concept . The obtained pressure drop in a three stage FBR was lower than in a single‐stage FBR . Thus, the appropriate design of a stage FBR will optimize the conversion efficiency and selectivity of the chemical reaction, as well as the superficial velocity of the reactant gas and catalyst solid particle, the volume fraction of the catalyst solid particle, gas turbulence, residence time, initial coke of catalyst, and the system temperature .…”

Section: Introductionmentioning

confidence: 99%

“…[29][30][31] The obtained pressure drop in a three stage FBR was lower than in a single-stage FBR. 32 Thus, the appropriate design of a stage FBR will optimize the conversion efficiency and selectivity of the chemical reaction, as well as the superficial velocity of the reactant gas and catalyst solid particle, the volume fraction of the catalyst solid particle, gas turbulence, residence time, initial coke of catalyst, and the system temperature. 32,33 With these advantages of including a stage in a FBR, a stage was then applied to the riser of a CFBR to improve the system hydrodynamics and chemical reaction behaviors.…”

Section: Introductionmentioning

confidence: 99%

Computational fluid dynamics simulation of system hydrodynamics in a riser of stage circulating fluidized bed reactor

Phupanit

Soanuch

Korkerd

et al. 2018

Asia-Pacific J Chem Eng

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The riser of conventional and stage circulating fluidized bed reactors were simulated using computational fluid dynamics. The objective was to examine the design parameter effects using a 23 statistical experimental design method. The results showed that number of reactor stages had the highest effect on the standard deviation of the solid volume fraction (SVF), the average SVF, and standard deviation of gas temperature in a horizontal direction. In addition, the reactor wall temperature had the highest effect on the average holding time of catalysts. Increasing the number of reactor stages could reduce the back‐mixing and increase the system turbulence. The average vertical and horizontal solid particle velocities in the reactor stage region were higher than in the other regions. At the reactor stage region, peaks in the gas temperature were observed. The advantages of a stage reactor were confirmed to be applied in all the operating condition cases, independent of the solid particle mass flux.

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Heterogeneous catalysis in multi‐stage fluidized bed reactors: From fundamental study to industrial application

et al. 2019

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The multi-stage fluidized bed (MSFB) reactor with several stages connected in series prevents gas and solids back-mixing effectively and obtains the plug-flow reactor performance. Besides, different process steps can be accomplished in a single reactor by establishing different temperatures and/or concentrations in each stage. Therefore, multi-stage fluidized bed reactors are acknowledged as novel and flexible multi-phase flow reactors for heterogeneous catalytic processes, especially with the intermediates as the desired products. Typical process developments in the industry involve the methanol to aromatics (MTA), regeneration in fluid catalytic cracking (FCC), and hydrogenation of nitrobenzene to aniline. The purpose of this article is to provide a comprehensive review of the fundamental research as well as particular industrial applications on multi-stage fluidized bed reactors in the Fluidization Laboratory of Tsinghua University (FLOTU).

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Design of a two-stage fluidized bed reactor for preparation of diethyl oxalate from carbon monoxide

Cited by 14 publications

References 38 publications

Iterative Multiscale Computational Fluid Dynamics–Single-Particle Model for Intraparticle Transfer and Catalytic Hydrogenation Reaction of Dimethyl Oxalate in a Fluidized-Bed Reactor

Iterative Multiscale Computational Fluid Dynamics–Single-Particle Model for Intraparticle Transfer and Catalytic Hydrogenation Reaction of Dimethyl Oxalate in a Fluidized-Bed Reactor

Computational fluid dynamics simulation of system hydrodynamics in a riser of stage circulating fluidized bed reactor

Heterogeneous catalysis in multi‐stage fluidized bed reactors: From fundamental study to industrial application

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