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arXiv:2604.26695 · detector doi_compliance · incontrovertible · 2026-05-19 19:55:45.065282+00:00

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H. Dhaouadi, S. Poncin, J. Hornut, N. Midoux, Gas–liquid mass transfer in bubble column reactor: Analytical solution and experimental confirmation, Chemical Engineering and Pro- cessing: Process Intensification 47 (4) (2008) 548–556.doi:10.1016/j.cep.2006.11. 009. URLhttps://linkinghub.elsevier.com/retrieve/pii/S0255270106002984 Appendix A. Simulation Parameters Table A.2 shows the simulation parameters. These parameters were also used for the com- partment model. We also assume same heat capacity of oxigen in the liquid and in the gas phase so that temperature canges can be neglected. 30 Table A.2: Simulation parameters Variable Value uin 0.05 [m/s] Le 70 [−] Sct 0.7 [−] Prliq 7.0 [−] Prgas 0.7 [−] MW O2 32.0 [kg/kmol] MW H2O 18.0 [kg/kmol] µliq 1×10 −3 [Pa s] dliq 1×10 −4 [m] dgas 3×10 −3 [m] ptot 1×10 5 [Pa] T293.15 [K] H∗ O2 in H 2O 3.45×10 −2 [−] ,[26] ρliq 1×10 3 [kg/m3 ρgas (calculated) 1.31 [kg/m 3] resolution 120 [nodes/m] domain size 0.2 x 1 x 0.1[m] turbulencekϵ-model solver reactingTwoPhaseEulerFoam drag model Schiller-Naumann, [27] mass transfer model Frössling, [28] Appendix B. Analytical Solutions In this section, analytical solutions are derived for the concentration distribution of a chem- ical species undergoing a first-order reaction within a two-dimensional channel flow between two infinite parallel plates. These analytical benchmarks are essential for the verification of the numerical models presented later in this work. Four distinct flow profiles are co

Evidence payload

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  "reconstructed_doi": "10.1016/j.cep.2006.11.009.URLhttps://linkinghub.elsevier.com/retrieve/pii/S0255270106002984",
  "ref_index": 29,
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