Modelling and experimental validation of a CO<sub>2</sub> methanation annular cooled fixed‐bed reactor exchanger

Ducamp, Julien; Bengaouer, Alain; Baurens, Pierre

doi:10.1002/cjce.22706

Cited by 54 publications

(36 citation statements)

References 19 publications

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“…This contact thermal resistance is a transport property attributed to the gas phase but it is introduced to represent the contact resistance between the fixed‐bed and the wall in a similar way

λ_{e q}

represents the heat transfer within the fixed‐bed. The heat transfer coefficient corresponding to this contact thermal resistance is taken from Ducamp's work on the same catalyst:

N u = \frac{α_{w} . d_{p}}{λ_{f}} = 0.345 . {(\frac{λ_{normals}}{λ_{normalf}})}^{0.75} + 3.95 . R e_{p}^{0.46} {P r}^{0.72}

…”

Section: Modeling Of the Single Channel Fixed‐bed Reactor‐exchangermentioning

confidence: 99%

“…In order to calculate the effective Knudsen diffusion coefficient, a value of three for the pores tortuosity is calculated using the Currie correlation corrected by Wakao and Smith . The considered value of the catalyst internal porosity

ɛ_{s}

, equal to 0.59, was taken from literature measurements on the same catalyst and the value of the particle density, 1274 kg.m −3 , found in the literature . The mass and energy balances in the catalyst phase are written as follow:

normalC normalo normalm normalp normalo normaln normale normaln normalt i normalm normala normals normals normalb normala normall normala normaln normalc normale : \frac{\partial C_{i, s}}{\partial t} + \nabla . (|, - D_{i, K} \nabla C_{i, s}) = ρ_{s} \sum_{normalj} ν_{i, j} . r_{j}

{E n e r g y b a l a n c e : ρ}_{s} C p_{s} \frac{\partial T_{s}}{\partial t} + \nabla . (|, - λ_{s} \nabla T_{s}) = ρ_{s} \sum_{normalj} true(- Δ_{r} H_{j} true) . r_{...}

…”

Section: Modeling Of the Single Channel Fixed‐bed Reactor‐exchangermentioning

confidence: 99%

“…Xu and Froment kinetic model was used with adapted parameters by Ducamp . This model takes into account the CO 2 methanation reaction, the CO methanation reaction and the Reverse Water Gas Shift reaction:

r_{C O 2} = - \frac{k_{{normalC normalO}_{2}}}{P_{{normalH}_{2}}^{3.5}} (|, P_{{normalC normalH}_{4}} P_{{normalH}_{2} O}^{2} - K_{e q, {normalC normalO}_{2}} P_{{normalH}_{2}}^{4} P_{{normalC normalO}_{2}}) \frac{1}{D e n^{2}}

r_{C O} = - \frac{k_{C O}}{P_{{normalH}_{2}}^{2.5}} (|, P_{{normalC normalH}_{4}} P_{{normalH}_{2} O} - K_{e q, C O} P_{{normalH}_{2}}^{3} P_{C O}) \frac{1}{D e n^{2}}

r_{R W}

…”

Section: Modeling Of the Single Channel Fixed‐bed Reactor‐exchangermentioning

confidence: 99%

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Dynamic modeling and simulations of the behavior of a fixed‐bed reactor‐exchanger used for CO₂ methanation

et al. 2017

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A multidimensional heterogeneous and dynamic model of a fixed-bed heat exchanger reactor used for CO 2 methanation has been developed in this work that is based on mass, energy and momentum balances in the gas phase and mass and energy balances for the catalyst phase. The dynamic behavior of this reactor is simulated for transient variations in inlet gas temperature, cooling temperature, gas inlet flow rate, and outlet pressure. Simulation results showed that wrong-way behaviors can occur for any abrupt temperature changes. Conversely, temperature ramp changes enable to attenuate and even fade the wrong-way behavior. Traveling hot spots appear only when the change of an operating condition shifts the reactor from an ignited steady state to a non-ignited one. Inlet gas flow rate variations reveal overshoots and undershoots of the reactor maximum temperature.2) Wall thermal conductivity, k w (stainless steel) 17 W m 21 K 21 Catalyst thermal conductivity, k s 9 0.87 W m 21 K 21 Catalyst particle density, q s 58 1274 kg m 23 472

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λ_{e q}

represents the heat transfer within the fixed‐bed. The heat transfer coefficient corresponding to this contact thermal resistance is taken from Ducamp's work on the same catalyst:

N u = \frac{α_{w} . d_{p}}{λ_{f}} = 0.345 . {(\frac{λ_{normals}}{λ_{normalf}})}^{0.75} + 3.95 . R e_{p}^{0.46} {P r}^{0.72}

…”

Section: Modeling Of the Single Channel Fixed‐bed Reactor‐exchangermentioning

confidence: 99%

ɛ_{s}

normalC normalo normalm normalp normalo normaln normale normaln normalt i normalm normala normals normals normalb normala normall normala normaln normalc normale : \frac{\partial C_{i, s}}{\partial t} + \nabla . (|, - D_{i, K} \nabla C_{i, s}) = ρ_{s} \sum_{normalj} ν_{i, j} . r_{j}

{E n e r g y b a l a n c e : ρ}_{s} C p_{s} \frac{\partial T_{s}}{\partial t} + \nabla . (|, - λ_{s} \nabla T_{s}) = ρ_{s} \sum_{normalj} true(- Δ_{r} H_{j} true) . r_{...}

…”

Section: Modeling Of the Single Channel Fixed‐bed Reactor‐exchangermentioning

confidence: 99%

r_{C O 2} = - \frac{k_{{normalC normalO}_{2}}}{P_{{normalH}_{2}}^{3.5}} (|, P_{{normalC normalH}_{4}} P_{{normalH}_{2} O}^{2} - K_{e q, {normalC normalO}_{2}} P_{{normalH}_{2}}^{4} P_{{normalC normalO}_{2}}) \frac{1}{D e n^{2}}

r_{C O} = - \frac{k_{C O}}{P_{{normalH}_{2}}^{2.5}} (|, P_{{normalC normalH}_{4}} P_{{normalH}_{2} O} - K_{e q, C O} P_{{normalH}_{2}}^{3} P_{C O}) \frac{1}{D e n^{2}}

r_{R W}

…”

Section: Modeling Of the Single Channel Fixed‐bed Reactor‐exchangermentioning

confidence: 99%

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Dynamic modeling and simulations of the behavior of a fixed‐bed reactor‐exchanger used for CO₂ methanation

et al. 2017

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“…This can be attributed to ongoing heat release by chemical reactions and low thermal conductivity in the gas phase. The thermal conductivity of the fixed‐bed reactor might be underestimated by the used thermal conductivity model as shown in .…”

Section: Simulation Resultsmentioning

confidence: 99%

Applying Reaction Kinetics to Pseudohomogeneous Methanation Modeling in Fixed‐Bed Reactors

et al. 2020

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Reactor simulations can reduce the effort when designing fixed-bed reactors for methanation processes. Several microkinetic models were developed under a variety of operating conditions. However, most production-scale fixed-bed methanation processes exceed the temperature range in which these kinetic models were obtained. In addition, heat and mass transport limitations strongly influence the reaction kinetics. In this work, microkinetic rate equations for CO and CO 2 methanation were analyzed with respect to their suitability for high-temperature, pseudohomogeneous reactor modeling. The best-suited kinetic model was fitted to the operating conditions and validated by means of CFD simulations. It is shown that the simulations match the experimental data for various operating conditions.

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“…As alreadym entioned above,i nt erms of heat evacuation, for the samek ind of experimental setup and under similar conditions,t he aluminum OCF catalyst showed ab etter heat evacuation capacity.W em easured am aximumt emperature increaseo f2 58C, whereas ap owder bed of this size showed temperature increases up to 200-250 8Cu nder similar conditions. [31] Deactivation of the catalyst through sinterings hould therefore be lower or negligible for the catalyst deposited on the OCF compared with that of powderc atalysts.…”

Section: Foam Versus Powder Bedmentioning

confidence: 99%

Aluminum Open Cell Foams as Efficient Supports for Carbon Dioxide Methanation Catalysts: Pilot‐Scale Reaction Results

et al. 2017

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To control the highly exothermal nature of carbon dioxide methanation (ΔRH=−165 kJ mol−1), a reactor capable of efficiently evacuating the heat generated is essential. A pilot‐scale (≈75 cm3) structured bed filled with an aluminum open cell foam (OCF) was chosen for the many advantages of this kind of reactor (high surface/volume ratio, low pressure drop, intensification of mass and heat transfer). A coating procedure for aluminum OCF was first developed. Different catalytic test conditions allowed a low temperature increase with a maximal value of 25 °C, as well as the influence of reaction temperature, pressure and flow rate on the axial temperature profile along the bed, to be shown. Finally, a comparison of the data collected herein for a powder fixed bed shows that the methane productivity obtained is similar to that obtained for the same catalyst in the powder form, but a much lower temperature increase due to the reaction and a lower pressure drop where clearly observed when using the aluminum OCF‐supported catalyst.

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Modelling and experimental validation of a CO₂ methanation annular cooled fixed‐bed reactor exchanger

Cited by 54 publications

References 19 publications

Dynamic modeling and simulations of the behavior of a fixed‐bed reactor‐exchanger used for CO₂ methanation

Dynamic modeling and simulations of the behavior of a fixed‐bed reactor‐exchanger used for CO₂ methanation

Applying Reaction Kinetics to Pseudohomogeneous Methanation Modeling in Fixed‐Bed Reactors

Aluminum Open Cell Foams as Efficient Supports for Carbon Dioxide Methanation Catalysts: Pilot‐Scale Reaction Results

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Modelling and experimental validation of a CO2 methanation annular cooled fixed‐bed reactor exchanger

Cited by 54 publications

References 19 publications

Dynamic modeling and simulations of the behavior of a fixed‐bed reactor‐exchanger used for CO2 methanation

Dynamic modeling and simulations of the behavior of a fixed‐bed reactor‐exchanger used for CO2 methanation

Applying Reaction Kinetics to Pseudohomogeneous Methanation Modeling in Fixed‐Bed Reactors

Aluminum Open Cell Foams as Efficient Supports for Carbon Dioxide Methanation Catalysts: Pilot‐Scale Reaction Results

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Product

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Modelling and experimental validation of a CO₂ methanation annular cooled fixed‐bed reactor exchanger

Dynamic modeling and simulations of the behavior of a fixed‐bed reactor‐exchanger used for CO₂ methanation

Dynamic modeling and simulations of the behavior of a fixed‐bed reactor‐exchanger used for CO₂ methanation