Hydrodynamics and mass transfer in trickle-bed reactors: an overview

Iliuta, Ion; Ortiz-Arroyo, Arturo; Larachi, Faı̈çal; Grandjean, Bernard P. A.; Wild, Gabriel

doi:10.1016/s0009-2509(99)00259-6

Cited by 63 publications

(56 citation statements)

References 19 publications

Supporting

Mentioning

Contrasting

Unclassified

Order By: Relevance

“…To report the selectivity, the usage ratio, recycle performance and cooling effect are investigated. Others (Iliuta, et al, 1999) take a view on the trickle-bed reactor's mass transfer and fluid dynamics characteristics, on the basis of investigating flow regime database.…”

Section: F-t Reactor Designmentioning

confidence: 99%

Simulation, integration, and economic analysis of gas-to-liquid processes

Bao

El‐Halwagi

Elbashir

2010

Fuel Processing Technology

156

103

View full text Add to dashboard Cite

Simulation, Integration, and Economic Analysis of Gas-to-Liquid Processes. (December 2008) Buping Bao, B.S., Zhejiang University Chair of Advisory Committee: Dr. Mahmoud M. El-Halwagi Gas-to-liquid (GTL) process involves the chemical conversion of natural gas (or other gas sources) into synthetic crude that can be upgraded and separated into different useful hydrocarbon fractions including liquid transportation fuels. A leading GTL technology is the Fischer Tropsch process. The objective of this work is to provide a techno-economic analysis of the GTL process and to identify optimization and integration opportunities for cost saving and reduction of energy usage and environmental impact. First, a basecase flowsheet is synthesized to include the key processing steps of the plant. Then, computer-aided process simulation is carried out to determine the key mass and energy flows, performance criteria, and equipment specifications. Next, energy and mass integration studies are performed to address the following items: (a) heating and cooling utilities, (b) combined heat and power (process cogeneration), (c) management of process water, (c) optimization of tail-gas allocation, and (d) recovery of catalystsupporting hydrocarbon solvents. Finally, an economic analysis is undertaken to determine the plant capacity needed to achieve the break-even point and to estimate the return on investment for the base-case study. After integration, 884 million $/yr is saved from heat integration, 246 million $/yr from heat cogeneration, and 22 million $/yr from water management. Based on 128,000 barrels per day (BPD) of products, at least 68,000 BPD capacity is needed to keep the process profitable, with the return on investment (ROI) of 5.1%. Compared to 8 $/1000 SCF natural gas, 5 $/1000 SCF price can increase the ROI to 16.2%.

show abstract

Section: F-t Reactor Designmentioning

confidence: 99%

Simulation, integration, and economic analysis of gas-to-liquid processes

Bao

El‐Halwagi

Elbashir

2010

Fuel Processing Technology

156

103

View full text Add to dashboard Cite

show abstract

“…These hydrodynamic parameters concern the two-phase pressure gradient, the flow regime transitions, the gas and liquid hold-ups in fixed and fluidized beds, the axial dispersion coefficients, the minimum fluidization velocity, and the bed porosity. The recent reviews by Dudukovic et al [68], Iliuta et al [69] and Larachi et al [70,71] can be consulted for retrieving some of the best correlations for estimation of the above discussed hydrodynamic parameters. Furthermore, several of these correlations can be directly downloaded from http://www.gch.ulaval.ca/flarachi.…”

Section: Hydrodynamic Parametersmentioning

confidence: 99%

Catalytic wet oxidation: micro–meso–macro methodology from catalyst synthesis to reactor design

Larachi

2005

Top Catal

View full text Add to dashboard Cite

Compared to alternative mature wet oxidation technologies that have tremendously proliferated in industry, heterogeneously mediated catalytic wet oxidation (CWO) has achieved, thus far, poor commercial penetration. The two factors that are likely responsible for this situation are (i) the lack of efficient and robust catalysts that pass with success the acid-test for commercial exploitation remote from the aseptic academic conditions, (ii) and the lack of a comprehensive reactor design framework and methodology for scale-up, reactor selection and operation inherent to the multiphase nature of the CWO reactors. This synthetic review summarizes the recent research and development work conducted at Laval University on the CWO from both the perspectives of catalyst development and testing, and multiphase reactor simulations and selection. Specific emphasis was put, on the one hand, on the development brought to some manganese oxide-ceria composites against deactivation, and on the other hand, on the formulation of multidimensional unsteady-steady non-isothermal mass-energy transport/reaction models, embedding catalyst deactivation or not, for trickle bed reactors, packed bubble column reactors, three-phase fluidized beds and slurry bubble columns. A micro-Meso-macro scale methodology was adopted from the materials synthesis up to reactor selection in which the catalyst performance (conversion, selectivity, and deactivation), the intrinsic chemical kinetics, the fluid phase thermodynamics, the pellet scale transport, and the reactor scale physical phenomena (heat, mass transport and hydrodynamics) were integrated. As a result, several aspects relevant to reactor behaviour such as solvent evaporation due to CWO reaction exothermic effects, catalyst partial wetting and catalyst deactivation, and back-mixing effects were covered, and recommendations were formulated. NomenclatureA reactor cross-sectional area, m 2 C concentration, mol/m 3 or g/L C p isobaric specific heat capacity, J/kg/K D eff effective diffusivity, m 2 /s E activation energy, kJ/mol E z axial dispersion coefficient, m 2 /s H Henry constant, or bed height, m H j hidden layer transfer function, k rate constants, mol/min/kg cat. (equations (1)-Arrhenius pre-exponential factor, mol/min/kg cat. equation (9) ka ll liquid-liquid volumetric mass transfer coefficient. s )1 k l a gas-liquid volumetric mass transfer coefficient, s )1 ka sls liquid-solid mass transfer coefficient, s )1 K adsorption equilibrium constant, m 3 /mol L v water enthalpy of vaporization, J/mol [m c ] catalyst loading, kg cat./m 3 P pressure, atm r spherical co-ordinate at pellet scale, m r c chemical reaction rate, mol/m 3 /s S neural network output S M mineralization selectivity t time, min T absolute temperature, K U i neural network inputs U superficial velocity, m/s v molar volume, cm 3 /mol [W] carbonaceous deposit carbon concentration, mol C/m 3 solution x dissolved mole fraction X chemical conversion y gas mole fraction z longitudinal co-ordinate, mGreek a deactivation function, DH...

show abstract

“…The form of bubble flow in porous media is not as familiar to people, although fluidized beds and packed-bed reactors with upward gas flow are well-known chemical processing techniques (Iliuta et al, 1999). We limit our consideration to the case where the solid grains are not disturbed by the bubble flow, and we present in Fig.…”

Section: Terminologymentioning

confidence: 99%

Leakage and Sepage of CO2 from Geologic Carbon SequestrationSites: CO2 Migration into Surface Water

Oldenburg¹,

Lewicki²

2005

View full text Add to dashboard Cite

Hydrodynamics and mass transfer in trickle-bed reactors: an overview

Cited by 63 publications

References 19 publications

Simulation, integration, and economic analysis of gas-to-liquid processes

Simulation, integration, and economic analysis of gas-to-liquid processes

Catalytic wet oxidation: micro–meso–macro methodology from catalyst synthesis to reactor design

Leakage and Sepage of CO2 from Geologic Carbon SequestrationSites: CO2 Migration into Surface Water

Contact Info

Product

Resources

About