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Publié le 14 mars 2023

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1

Nosek, Radovan, Jozef Jandacka et Andrzej Szlek. « Boiler Modelling of Simple Combustion Processes ». International Journal of Energy Optimization and Engineering 1, no 3 (juillet 2012) : 96–119. http://dx.doi.org/10.4018/ijeoe.2012070105.

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The aim of the work is to investigate coal combustion in fixed bed reactor. The experimental results were worked out in the form of approximation functions describing gas composition at the exit of fixed bed reactor. Furthermore, developed functions were applied for defining the boundary conditions at the interface between the fixed bed and gas phase using FLUENT. The simulations of a domestic boiler have been done and the relative effects of different factors in CFD code were evaluated by sensitivity analysis. The validity of the model was verified by measurements which were done in a 25 kW domestic boiler. Model predictions were compared with the experimental gas temperature and species concentration measurements.
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2

Bell, N. H., et T. F. Edgar. « Modelling of a fixed-bed water-gas shift reactor ». Journal of Process Control 1, no 2 (mars 1991) : 59–67. http://dx.doi.org/10.1016/0959-1524(91)80002-2.

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3

Bell, N. H., et T. F. Edgar. « Modelling of a fixed-bed water-gas shift reactor ». Journal of Process Control 1, no 1 (janvier 1991) : 22–31. http://dx.doi.org/10.1016/0959-1524(91)87004-h.

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4

Dhaundiyal, Alok, Suraj B. Singh et Istvan Bacskai. « Mathematical Modelling of Pyrolysis of Hardwood (Acacia) ». Acta Technologica Agriculturae 23, no 4 (1 décembre 2020) : 176–82. http://dx.doi.org/10.2478/ata-2020-0028.

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AbstractThis paper emphasises the analogous modelling of hardwood (acacia) pyrolysis. The impacts of physical characteristics of hardwood chips on the pyrolysis are examined through the conservation of biomass solid mass fraction. The ONORM standard chips of sizes ‘G30’ and ‘G50’ and their combination are individually tested in the pyrolysis reactor. In the analogous situation, the fixed bed is assumed to be a wooden slab with a porosity equivalent to the voidage of bed. Bulk density, bed length and porosity are several of the physical attributes of a fixed bed used to examine the variation in the hardwood solid mass across the fixed bed. To measure temperature, the four-temperature sensors separated from each other by 80 mm are fixed along periphery of a reactor. The heating element of 2 kWe is provided to initiate the biomass pyrolysis. The proposed model is also used to establish the relationship between the kinetics of pyrolysis and the structural properties of hardwood.
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5

Ching, C. B., et K. H. Chu. « Modelling of a fixed bed and a fluidized bed immobilized enzyme reactor ». Applied Microbiology and Biotechnology 29, no 4 (octobre 1988) : 316–22. http://dx.doi.org/10.1007/bf00265813.

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6

Dixon, Anthony G. « Fixed bed catalytic reactor modelling-the radial heat transfer problem ». Canadian Journal of Chemical Engineering 90, no 3 (28 décembre 2011) : 507–27. http://dx.doi.org/10.1002/cjce.21630.

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7

Dhaundiyal, Alok, et Suraj Bhan Singh. « Mathematical Modelling of Volatile Gas Using Lattice Boltzmann Method ». Environmental and Climate Technologies 24, no 1 (1 janvier 2020) : 483–500. http://dx.doi.org/10.2478/rtuect-2020-0030.

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AbstractThis study investigates the behaviour of pyrolysis gas, generated by the thermal decomposing of biomass, in a pilot size reactor. The discreet mathematical model, Lattice Boltzmann, has adopted for mathematical simulation of flow of pyrolysis gas across a porous bed of biomass. The effect of permeability, pressure gradient, voidage of bed, density, temperature, and the dynamic viscosity on the mass flow rate of gas is examined by simulating the gas flow across the fixed bed of hardwood. The Darcy equation is used to estimate the flow rate of gas across the fixed bed of hardwood chips. The temperature in the reactor varies from 32 °C to 600 °C. The reactor has an external diameter of 220 mm and the vertical height of 320 mm. Rockwool insulation is used to prevent heat loss across the reactor. The external heating element of 2 kWe was provided to trigger the pyrolysis reaction. The properties of the system have been recorded by the pressure and temperature sensors, which are retrofitted along the periphery of the reactor. The temperature sensors are located at 80 mm apart from each other; whereas the pressure sensor, placed at the bottom circumference of the reactor. The effect of input parameters on the flow properties of gas is also examined to add up the qualitative assessment of the system to biomass pyrolysis. The polytropic equation of gas is found to be PV2.051 = C, whereas the compressibility of gas varies from 0.0025–0.042 m2·N–1.
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8

Acharya, D. R., et R. Hughes. « Modelling of butene-1 dehydrogenation in a fixed bed reactor - bed and pellet profiles ». Canadian Journal of Chemical Engineering 68, no 1 (février 1990) : 89–96. http://dx.doi.org/10.1002/cjce.5450680111.

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9

Zhapbasbayev, U. K., G. I. Ramazanova et O. B. Kenzhaliev. « Modelling of turbulent flow in a radial reactor with fixed bed ». Thermophysics and Aeromechanics 22, no 2 (mars 2015) : 229–43. http://dx.doi.org/10.1134/s0869864315020092.

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10

Ciambelli, P., A. Di Benedetto, R. Pirone et G. Russo. « Spontaneous isothermal oscillations in N2O catalytic decomposition : fixed-bed reactor modelling ». Chemical Engineering Science 54, no 20 (octobre 1999) : 4521–27. http://dx.doi.org/10.1016/s0009-2509(99)00162-1.

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11

Xiao, Wen-De, et Wei-Kang Yuan. « Modelling and simulation for adiabatic fixed-bed reactor with flow reversal ». Chemical Engineering Science 49, no 21 (1994) : 3631–41. http://dx.doi.org/10.1016/0009-2509(94)00163-4.

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12

Hu, Rui-zhu, Ting-lin Huang, Gang Wen et Shang-ye Yang. « Modelling particle growth of calcium carbonate in a pilot-scale pellet fluidized bed reactor ». Water Supply 17, no 3 (30 septembre 2016) : 643–51. http://dx.doi.org/10.2166/ws.2016.158.

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Pellet fluidized bed reactors have been widely used to soften water. Reports from laboratory-scale research on the particle growth kinetics of calcium carbonate in pellet reactors have been put forward. However, the reports have not been comprehensive as they only consider the influence of supersaturation on the calcium carbonate growth process. The influence of three factors, namely, the superficial velocity (SV), particle size (L0), and supersaturation (S) on the particle growth rate of calcium carbonate were investigated in a pilot-scale study, and two models of particle growth rate and fixed bed height growth rate were built. The linear particle growth model G = 3.90 × 10−SV1.93L0−1.56S2.13 at the bottom of the pellet reactor was built based on a pilot-scale study of particle growth kinetics influenced by SV, L0, and S. The growth of the fixed bed height is closely related to the particle growth and also influenced by the three factors. The fixed bed growth model Rh = 5.19 × 10−8SV1.65L0−0.93S2.58 also incorporates SV, L0, and S, and provides a method for calculating the fixed bed height. The two models were built based on the pilot-scale experiment and were different from those previously reported. They are applicable as pellet discharge guides and are used in the management of pellet reactors.
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13

Szukiewicz, M., K. Kaczmarski et R. Petrus. « Modelling of fixed-bed reactor : two models of industrial reactor for selective hydrogenation of acetylene ». Chemical Engineering Science 53, no 1 (janvier 1998) : 149–55. http://dx.doi.org/10.1016/s0009-2509(97)00282-0.

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14

Alexiadis, A., G. Baldi et I. Mazzarino. « Modelling of a photocatalytic reactor with a fixed bed of supported catalyst ». Catalysis Today 66, no 2-4 (mars 2001) : 467–74. http://dx.doi.org/10.1016/s0920-5861(01)00255-3.

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15

Pereira, Carla S. M., Viviana M. T. M. Silva et Alírio E. Rodrigues. « Fixed Bed Adsorptive Reactor for Ethyl Lactate Synthesis : Experiments, Modelling, and Simulation ». Separation Science and Technology 44, no 12 (24 août 2009) : 2721–49. http://dx.doi.org/10.1080/01496390903135865.

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16

Hwang, Young Bo, et D. Dochain. « Dynamical Modelling of a Biological Detoxication Process in a Fixed Bed Reactor ». IFAC Proceedings Volumes 28, no 3 (mai 1995) : 148–53. http://dx.doi.org/10.1016/s1474-6670(17)45617-5.

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17

Ravella, Alberto, Hugo I. De Lasa et Arnaud Mahay. « Pseudoadiabatic axial thermal profiles in a catalytic fixed-bed reactor : Measurements and modelling ». Chemical Engineering Journal 42, no 1 (octobre 1989) : 7–15. http://dx.doi.org/10.1016/0300-9467(89)80002-4.

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18

Rout, Kumar R., et Hugo A. Jakobsen. « A numerical study of fixed bed reactor modelling for steam methane reforming process ». Canadian Journal of Chemical Engineering 93, no 7 (4 juin 2015) : 1222–38. http://dx.doi.org/10.1002/cjce.22202.

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19

Ducamp, Julien, Alain Bengaouer et Pierre Baurens. « Modelling and experimental validation of a CO2methanation annular cooled fixed-bed reactor exchanger ». Canadian Journal of Chemical Engineering 95, no 2 (2 novembre 2016) : 241–52. http://dx.doi.org/10.1002/cjce.22706.

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20

Atalay, Suheyda, et H. Erden Alpay. « Modelling of a Fixed Bed Reactor for the Air Oxidation of 1,2-Dichlorobenzene ». Chemie Ingenieur Technik 59, no 2 (février 1987) : 176–77. http://dx.doi.org/10.1002/cite.330590235.

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21

Chaudhari, R. V., R. Jaganathan, S. H. Vaidya, S. T. Chaudhari, R. V. Naik et C. V. Rode. « Hydrogenation of diethyl maleate in a fixed-bed catalytic reactor : kinetics, reactor modelling and pilot plant studies ». Chemical Engineering Science 54, no 15-16 (juillet 1999) : 3643–51. http://dx.doi.org/10.1016/s0009-2509(98)00511-9.

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22

Browning, B., I. Pitault, N. Sheibat-Othman, E. Tioni, V. Monteil et T. F. L. McKenna. « Dynamic modelling of a stopped flow fixed bed reactor for gas phase olefin polymerisation ». Chemical Engineering Journal 207-208 (octobre 2012) : 635–44. http://dx.doi.org/10.1016/j.cej.2012.07.027.

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23

Atashi, Hossein, et Fatemeh Rezaeian. « Modelling and optimization of Fischer–Tropsch products through iron catalyst in fixed-bed reactor ». International Journal of Hydrogen Energy 42, no 23 (juin 2017) : 15497–506. http://dx.doi.org/10.1016/j.ijhydene.2017.04.224.

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24

Grozev, Georgi G., et Christo G. Sapundzhiev. « Modelling of the reversed flow fixed bed reactor for catalytic decontamination of waste gases ». Chemical Engineering & ; Technology 20, no 6 (août 1997) : 378–83. http://dx.doi.org/10.1002/ceat.270200604.

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25

Roohi, Parham, Reza Alizadeh, Esmaeil Fatehifar et Mehdi Salami Hosseini. « Application of Finite Element Method for Modeling of Multi-tube Fixed Bed Catalytic Reactors ». Chemical Product and Process Modeling 9, no 1 (1 juin 2014) : 1–8. http://dx.doi.org/10.1515/cppm-2013-0030.

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Abstract In this article, the finite element method (FEM) was applied for modeling of multi-tube fixed bed catalytic reactor (FBCR). For this purpose, a more sophisticated 2D pseudo-heterogeneous model was used to calculate steady-state temperature and partial pressure profiles through the reactor. This model has a vast capability in the prediction of temperature and partial pressure distribution, separately, in the fluid and catalyst phases. The finite element results were compared with de wasch and Froment’s numerical work which developed for a well-established reaction in the multi-tube FBCR (o-xylene partial oxidation). The R-squared analysis indicated that the FEM results agree favorably with finite difference results which reported in the literature. Numerical solution coincidence of FEM and FDM increases with reduction of inlet gas temperature. The results show that the finite element as a powerful numerical method can be used to describe the multi-tube fixed bed catalytic reactor.
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26

Ahn, Chang-Il, Yong Min Park, Jae Min Cho, Dong Hyun Lee, Chan-Hwa Chung, Bong Gyoo Cho et Jong Wook Bae. « Fischer-Trospch Synthesis on Ordered Mesoporous Cobalt-Based Catalysts with Compact Multichannel Fixed-Bed Reactor Application : A Review ». Catalysis Surveys from Asia 20, no 4 (6 octobre 2016) : 210–30. http://dx.doi.org/10.1007/s10563-016-9219-5.

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27

Gribovskiy, A. G., L. L. Makarshin, D. V. Andreev, S. P. Klenov et V. N. Parmon. « A compact highly efficient multichannel reactor with a fixed catalyst bed to produce hydrogen via methanol steam reforming ». Chemical Engineering Journal 231 (septembre 2013) : 497–501. http://dx.doi.org/10.1016/j.cej.2013.07.068.

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28

Bignami, L., B. Eramo, R. Gavasci, R. Ramadori et E. Rolle. « Modelling and Experiments on Fluidized-Bed Biofilm Reactors ». Water Science and Technology 24, no 7 (1 octobre 1991) : 47–58. http://dx.doi.org/10.2166/wst.1991.0184.

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Over the last few years considerable attention has been devoted to biological fluidized-bed technology which seems to be potentially more advantageous than both dispersed biomass processes and fixed bed systems. An obstacle to the spreading of this technology is the lack of rigorous criteria in designing reactors, due to the poor knowledge of interconnections of fluid-dynamic aspects with kinetic ones. This paper reviews the rational basis for reactor design and reports on the experimental tests carried out in order to gain a better understanding in the areas of biofilm modelling and fluidization mechanics. In particular a biofilm model, in the general case of the Michaelis and Menten equation, was developed and its validity was verified utilizing experimental data obtained in nitrifying batch tests. As to fluidization mechanics the experimental work confirms the Wen and Yu(1966) approach to correlate the bed porosity with the superficial liquid velocity.
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Baumann, Urs, et Markus T. Müller. « Determination of anaerobic biodegradability with a simple continuous fixed-bed reactor ». Water Research 31, no 6 (juin 1997) : 1513–17. http://dx.doi.org/10.1016/s0043-1354(96)00406-x.

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30

Lin, Yen-Hui. « Kinetics of nitrogen and carbon removal in a moving-fixed bed biofilm reactor ». Applied Mathematical Modelling 32, no 11 (novembre 2008) : 2360–77. http://dx.doi.org/10.1016/j.apm.2007.09.009.

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31

Huo, Guanping, et Xueyan Guo. « Numerical Analyses of Heterogeneous CLC Reaction and Transport Processes in Large Oxygen Carrier Particles ». Processes 9, no 1 (8 janvier 2021) : 125. http://dx.doi.org/10.3390/pr9010125.

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Heterogeneous chemical looping combustion (CLC) reactions and conjugate transports in large oxygen carrier particles were numerically investigated with computational fluid dynamics (CFD) approaches, in which a simplified noncatalytic reaction model was implemented for reducing intraparticle modelling computation. Volumic gas-solid reactions were treated as surface reactions based on the equivalent internal surface in the particle model. In large porous particles such as fixed bed CLC reactors, the heterogeneous reactions are often limited by intraparticle diffusion. Comprehensive analyses were conducted on transports across the particle surface and their influences on reactions inside the single particles. A threshold Reynolds number of external convections was found for the enhancement of intraparticle reactions. The heterogeneous reactions, intraparticle diffusions and interstitial transports in a fixed bed CLC reactor randomly packed with 597 spheres were thoroughly analysed with the same numerical approaches. Comprehensive insights of the temporal evolution and spatial distribution of scalars in the packed bed reactor were presented.
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Huo, Guanping, et Xueyan Guo. « Numerical Analyses of Heterogeneous CLC Reaction and Transport Processes in Large Oxygen Carrier Particles ». Processes 9, no 1 (8 janvier 2021) : 125. http://dx.doi.org/10.3390/pr9010125.

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Heterogeneous chemical looping combustion (CLC) reactions and conjugate transports in large oxygen carrier particles were numerically investigated with computational fluid dynamics (CFD) approaches, in which a simplified noncatalytic reaction model was implemented for reducing intraparticle modelling computation. Volumic gas-solid reactions were treated as surface reactions based on the equivalent internal surface in the particle model. In large porous particles such as fixed bed CLC reactors, the heterogeneous reactions are often limited by intraparticle diffusion. Comprehensive analyses were conducted on transports across the particle surface and their influences on reactions inside the single particles. A threshold Reynolds number of external convections was found for the enhancement of intraparticle reactions. The heterogeneous reactions, intraparticle diffusions and interstitial transports in a fixed bed CLC reactor randomly packed with 597 spheres were thoroughly analysed with the same numerical approaches. Comprehensive insights of the temporal evolution and spatial distribution of scalars in the packed bed reactor were presented.
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33

Winkler, Tom, Fabien Baccot, Kari Eränen, Johan Wärnå, Gerd Hilpmann, Rüdiger Lange, Markus Peurla et al. « Catalytic decomposition of formic acid in a fixed bed reactor – an experimental and modelling study ». Catalysis Today 387 (mars 2022) : 128–39. http://dx.doi.org/10.1016/j.cattod.2021.10.022.

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34

Mizsey, P., A. Cuellar, E. Newson, P. Hottinger, T. B. Truong et F. von Roth. « Fixed bed reactor modelling and experimental data for catalytic dehydrogenation in seasonal energy storage applications ». Computers & ; Chemical Engineering 23 (juin 1999) : S379—S382. http://dx.doi.org/10.1016/s0098-1354(99)80093-3.

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35

Benguerba, Yacine, Lila Dehimi, Mirella Virginie, Christine Dumas et Barbara Ernst. « Modelling of methane dry reforming over Ni/Al2O3 catalyst in a fixed-bed catalytic reactor ». Reaction Kinetics, Mechanisms and Catalysis 114, no 1 (10 septembre 2014) : 109–19. http://dx.doi.org/10.1007/s11144-014-0772-5.

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36

Jung, Hans Jürgen, et Werner Bauer. « Determination of process parameters and modelling of lipase-catalyzed transesterification in a fixed bed reactor ». Chemical Engineering & ; Technology 15, no 5 (octobre 1992) : 341–48. http://dx.doi.org/10.1002/ceat.270150509.

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37

Ajayi, Babajide Patrick, Basim Abussaud, Rabindran Jermy et Sulaiman Al Khattaf. « Kinetic Modelling of n-butane Dehydrogenation Over CrOxVOx/MCM-41 Catalyst in a Fixed Bed Reactor ». Progress in Reaction Kinetics and Mechanism 39, no 4 (décembre 2014) : 341–53. http://dx.doi.org/10.3184/146867814x14119972226885.

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38

Nehring, Dirk, Roberto Gonzalez, Ralf Pörtner et Peter Czermak. « Experimental and modelling study of different process modes for retroviral production in a fixed bed reactor ». Journal of Biotechnology 122, no 2 (mars 2006) : 239–53. http://dx.doi.org/10.1016/j.jbiotec.2005.09.014.

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39

Marín, Pablo, Fernando V. Díez et Salvador Ordóñez. « Fixed bed membrane reactors for WGSR-based hydrogen production : Optimisation of modelling approaches and reactor performance ». International Journal of Hydrogen Energy 37, no 6 (mars 2012) : 4997–5010. http://dx.doi.org/10.1016/j.ijhydene.2011.12.027.

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40

Pineda, Miguel, JoséM Palacios, Enrique García, Cristina Cilleruelo et JoséV Ibarra. « Modelling of performance of zinc ferrites as high-temperature desulfurizing sorbents in a fixed-bed reactor ». Fuel 76, no 7 (mai 1997) : 567–73. http://dx.doi.org/10.1016/s0016-2361(97)00070-7.

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41

Pollet, Eric, Thierry Hamaide, Melaz Tayakout-Fayolle et Christian Jallut. « Heterogeneous anionic ring opening polymerization in a fixed-bed reactor : description of the process and modelling ». Polymer International 53, no 5 (21 avril 2004) : 550–56. http://dx.doi.org/10.1002/pi.1431.

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42

Vanden Bussche, K. M., S. N. Neophytides, I. A. Zolotarskii et G. F. Froment. « Modelling and simulation of the reversed flow operation of a fixed-bed reactor for methanol synthesis ». Chemical Engineering Science 48, no 19 (octobre 1993) : 3335–45. http://dx.doi.org/10.1016/0009-2509(93)80150-o.

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43

Wang, Chengcheng, Hongkun Ma, Abdalqader Ahmad, Hui Yang, Mingxi Ji, Boyang Zou, Binjian Nie et al. « Discharging Behavior of a Fixed-Bed Thermochemical Reactor under Different Charging Conditions : Modelling and Experimental Validation ». Energies 15, no 22 (9 novembre 2022) : 8377. http://dx.doi.org/10.3390/en15228377.

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Thermochemical heat storage has attracted significant attention in recent years due to potential advantages associated with very high-energy density at the material scale and its suitability for long-duration energy storage because of almost zero loss during storage. Despite the potential, thermochemical heat storage technologies are still in the early stage of development and little has been reported on thermochemical reactors. In this paper, our recent work on the charging and discharging behavior of a fixed-bed thermochemical reactor is reported. Silica gels were used as the sorbent for the experimental work. An effective model was established to numerically study the effect of different charging conditions on the discharging behavior of the reactor, which was found to have a maximum deviation of 10.08% in terms of the root mean square error compared with the experimental results. The experimentally validated modelling also showed that the discharging temperature lift increased by 5.84 times by changing the flow direction of the air in the discharging process when the charging level was at 20%. At a charging termination temperature of 51.25 °C, the maximum discharging temperature was increased by 2.35 °C by reducing the charging flow velocity from 0.64 m/s to 0.21 m/s. An increase in the charging temperature and a decrease in the air humidity increased the maximum discharging outlet temperature lift by 3.37 and 1.89 times, respectively.
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44

Aksikas, I., L. Mohammadi, J. F. Forbes, Y. Belhamadia et S. Dubljevic. « Optimal control of an advection-dominated catalytic fixed-bed reactor with catalyst deactivation ». Journal of Process Control 23, no 10 (novembre 2013) : 1508–14. http://dx.doi.org/10.1016/j.jprocont.2013.09.016.

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Huang, Cheng-Hung, et Bo-Yi Li. « An inverse problem in estimating simultaneously the non-linear reaction rates for a fixed-bed reactor ». Applied Mathematical Modelling 39, no 8 (avril 2015) : 2217–33. http://dx.doi.org/10.1016/j.apm.2014.10.032.

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46

Karama, A., O. Bernard, J. L. Gouzé, A. Benhammou et D. Dochain. « Hybrid neural modelling of an anaerobic digester with respect to biological constraints ». Water Science and Technology 43, no 7 (1 avril 2001) : 1–8. http://dx.doi.org/10.2166/wst.2001.0375.

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A hybrid model for an anaerobic digestion process is proposed. The fermentation is assumed to be performed in two steps, acidogenesis and methanogenesis, by two bacterial populations. The model is based on mass balance equations, and the bacterial growth rates are represented by neural networks. In order to guarantee the biological meaning of the hybrid model (positivity of the concentrations, boundedness, saturation or inhibition of the growth rates) outside the training data set, a method that imposes constraints in the neural network is proposed. The method is applied to experimental data from a fixed bed reactor.
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47

Diglio, Giuseppe, Dawid P. Hanak, Piero Bareschino, Francesco Pepe, Fabio Montagnaro et Vasilije Manovic. « Modelling of sorption-enhanced steam methane reforming in a fixed bed reactor network integrated with fuel cell ». Applied Energy 210 (janvier 2018) : 1–15. http://dx.doi.org/10.1016/j.apenergy.2017.10.101.

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Kac, Feride Ulu, Mehmet Kobya et Erhan Gengec. « Removal of humic acid by fixed-bed electrocoagulation reactor : Studies on modelling, adsorption kinetics and HPSEC analyses ». Journal of Electroanalytical Chemistry 804 (novembre 2017) : 199–211. http://dx.doi.org/10.1016/j.jelechem.2017.10.009.

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Mejias Carpio, Isis E., Glaucia Machado-Santelli, Solange Kazumi Sakata, Sidney Seckler Ferreira Filho et Debora Frigi Rodrigues. « Copper removal using a heavy-metal resistant microbial consortium in a fixed-bed reactor ». Water Research 62 (octobre 2014) : 156–66. http://dx.doi.org/10.1016/j.watres.2014.05.043.

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Nouvion, N., J. C. Block et G. M. Faup. « Effect of biomass quantity and activity on TOC removal in a fixed-bed reactor ». Water Research 21, no 1 (janvier 1987) : 35–40. http://dx.doi.org/10.1016/0043-1354(87)90096-0.

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