Diffiision boundary layer

The mc l of fee diffiision boundary layer [4-7] also leads to fee same conclusion, xording to this model, both fee increasing of fee flow rate and fee... 

Nijsii [1964] Organic coolant in nuclear reactors Hydrodynamic boundary layer and diffusion partial differential equations Product diffiision back to the fluid bulk Solution with diffiision control fits plant data, fouling rate predicted to increase with velocity... 

Diffusion across aNemst boundary layer (thickness 6, diffiisivity D) produces the well-known convective-diffusion term ... 

From the hydrocarbon phase distributed in the aqueous phase as droplets, COS will be partitioned into the aqueous phase, and then a diffiision limited fast reaction will take place in the aqueous boundary layer. Since the rate of hydrolysis of COS in the aqueous phase by caustic soda depends also on the aqueous phase COS concentration, Ccas,w> increasing Cqh, u by increasing caustic soda concentration can lead to a reduction in ficos by reducing Ccos,i . An increase in the electrolyte (NaOH) concentration will reduce the COS solubility according to the Setch-enow (1892) relation. Further, COS diffiisivity will also be reduced as the caustic soda concentration is incretised. Dewitt (1980) has thereby demonstrated experimentally and theoretically that the COS extraction rate is maximum at an intermediate NaOH concentration. 

The same approach for the PGM phase modeling was adopted in the development of the mathematical model of Dual-Layer ASC monolith catalysts [20]. Such a model, named LSM (Layer + Surface Model), was based on the mathematical model for SCR monolithic converters [12,25,26]. As detailed in the following, the PGM reactivity was directly included in the mentioned SCR converter model by simply modifying the inner boundary condition for the diffiision- -eaction equations within the SCR layer, i.e., the boundary condition at the interface with the PGM phase. It is worth emphasizing that the LSM model reduces to the PGM monolith model when the SCR layer thickness approaches zero. 

One very attractive way to circumvent this problem is to apply the catalytic ionic liquid in the form of a supported thin film Such supported thin films provide the whole volume of the ionic catalyst solution close to the fluid-fluid phase boundary, thus within the diffiision layer. The realisation of this concept has been introduced into the literature under the term SILP catalysis. 

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