Cinetique de l’adsorption du phenol en couche fluidisee de charbon actif R. Ganho. Thèse Docteur-Ingénieur, Université Paul-Sabatier, Toulouse (). [17] . Etude de l’adsorption de complexes cyanures sur charbon actif .. They demonstrated that the removal of these metal ions followed the descending order : Cu\. Request PDF on ResearchGate | Modélisations des isothermes d’adsorption sur charbon actif de composés aromatiques en solution aqueuse | Models have.

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Low concentrations of organic contaminants are not easily removed by conventional treatment methods, but activated carbon bas a good affinity for various organics and is used in batch or column reactors.

Some investigators have attempted to simulate column performance with mathematical models and the aim of this work is to present the principal models and verify how the different models are applied to break-through curves ; parameters which can be evaluated by the different equations will also be compared. As early as BOHART and ADAMS presented differential equations which govern the dynamics of the adsorption of vapours and gases on fixed beds and the final result, applied to the liquid-solid phase, yields the kinetic adsorption rate k and the maximum adsorption tjeses No eq.


By transposition to the liquid phase, we have calculated the concentration distribution in the bed eq.

The activated carbon efficiency No can be estimated and the adsorption rate constant calculated from the slope and the y-intercept. The model developed by CLARK is based on the use of e mass-transfer concept in combination with the Freundlich isotherm fig.

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The general equation is equation Two parameters A and r are determined by regression equations ; we proposed a simple method to calculate A and r by a linearization of the preceding equation eq.

The linear flow rates were 3. The Freundlich isotherm equation fig.

The agreement is only for the low values of C in the break-through curves. The coefficients A and B table 1 are determined from the straight lines obtained with the low break-curve concentrations fig.

The kinetic coefficient Sa, and the maximum capacity adsorption No are shown in table 1.

The No value is similar to those obtained from the adsorptiom equations. The linearized Clark equation 16 gives a good representation of experimental results fig.

With the use of the two parameters, the break-through curves have been recalculated fig. Their is good agreement. The A parameter is related to the depth Z of the adsorbant: B value can be determined with the different columns fig.


From the difference in the area of the two curves, it charbob possible to calculate the supplementary biological degradation.

The percentage is constant alter 35 cm depth of the activated carton in agreement with the electon microscopy study that showed that the flora was only present in the 10 first centimeters.

Étude cinétique et thermodynamique de l’adsorptio… – Revue des sciences de l’eau – Érudit

The use of this model is facilitated by our linearization and the case of particular phenomena: In conclusion, nome of the tested models lead to different parameters by using low break-through curve concentrations or others with the whole range of experimental points, cbarbon only one CLARK gives a good description of the break-through curves in our actual knowledge. Mode, dynamic adsorption, activated carton, kinetic parameters, anionic surfactant, humic acids.

Adsorption dynamique en phase liquide sur charbon actif: Revue des sciences de l’eau6 163— Revue des sciences de l’eau 6, n o 1