Fuller's earth and fired clay as absorbents for dyestuffs external mass transport processes during adsorption

McKay, Gordon; Otterburn, M. S.; Aga, Jamal A.

doi:10.1007/bf00292065

Cited by 16 publications

(9 citation statements)

References 6 publications

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“…It is generally accepted that step 3 is quite rapid and does not represent the rate‐determining step in the uptake of the adsorbate compound . The main rate‐controlling step during the initial adsorption of the adsorbate onto a solid phase should be the external mass transport or film diffusion . Here, step 2 is considered to be about equally rapid with step 3, and therefore, it is not rate limiting in the kinetic studies undertaken in this work.…”

Section: Resultsmentioning

confidence: 99%

“…This mechanism is satisfied in accordance with the mass transfer theory of adsorption phenomena. It is generally accepted that step 3 is quite rapid and does not represent the rate‐determining step in the uptake of the adsorbate compound . The main rate‐controlling step during the initial adsorption of the adsorbate onto a solid phase should be the external mass transport or film diffusion .…”

Section: Resultsmentioning

confidence: 99%

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Adsorptive removal of biophenols from olive mill wastewaters (OMW) by activated carbon: mass transfer, equilibrium and kinetic studies

Şenol

Hasdemir

et al. 2016

Asia-Pacific J Chem Eng

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In this study, the removal of biophenols from olive mill wastewater by activated carbon of different particle sizes has been carried out using the batch adsorption technique. The effects of the sorbent specific surface area and concentration, temperature, initial biophenols concentration, and contact time on the adsorption efficiency have been analyzed independently. The sorbent yields higher removal efficiency of biophenols as its specific surface area increases. When increasing the sorbent concentration from 10 to 50 g L À1 , the sorbent uptake capacity increases from 20% to 41%, and it reaches a maximum value of 65 mg g À1 at 298.2 K. Adsorption of olive mill wastewater biophenols is moderately rapid, being about 38% to 40% of the initial phenolic content after 120 min. Kinetic analysis shows that the adsorption process can be approximated by a pseudo-second-order model for which pore diffusion is the essential rate-controlling step. Equilibrium modeling by linearized adsorption isotherms reveals that a Langmuir-type isotherm with a preferable monolayer sorption would likely proceed. Calculated thermodynamic parameters such as Gibbs energy, enthalpy, entropy, activation energy, and sticking probability indicate that adsorption is a typical endothermic yet spontaneous process with a preferable physisorption mechanism. An external mass transfer coefficient model has been developed to determine the rate of adsorption controlled initially by the boundary layer film, with particular focus on its predictive performance.

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Section: Resultsmentioning

confidence: 99%

Section: Resultsmentioning

confidence: 99%

Adsorptive removal of biophenols from olive mill wastewaters (OMW) by activated carbon: mass transfer, equilibrium and kinetic studies

Şenol

Hasdemir

et al. 2016

Asia-Pacific J Chem Eng

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“…Apart from the sorbent properties, such as the specific surface area and surface charge, pH and temperature may influence the sorption. The adsorption of dyes on clay minerals has been extensively studied in the past (McKay et al, 1985;Das & Chatterjee, 1993;Dogan et al, 2000;Bujdák et al, 2002;Li et al, 2011;Errais et al, 2012;Gunay et al, 2013;Auta & Hameed, 2014). However, only a few detailed studies have been conducted on the desorption of dyes from natural clay minerals (e.g.…”

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confidence: 99%

Adsorption-desorption processes of azo dye on natural bentonite: batch experiments and modelling

et al. 2014

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The purpose of this study was to determine whether a bentonite from the Gafsa deposit (western Tunisia) could be used to remove the Foron Blue 291 (FB) azo dye from wastewater. Batch adsorption and desorption experiments were conducted using untreated and purified bentonite and the influence of contact time, pH, adsorbent mass and temperature of the dye solution on the adsorption of FB was evaluated. Kinetic and isotherm data were fitted using two non-linear kinetic and two non-linear isotherm equations. In addition, the fits were evaluated using the coefficient of determination (R2) and the RMSE. The percentage of dye removal increased with increasing amount of adsorbent until total discolouration was achieved. The adsorption isotherms followed the Langmuir model, with the purified bentonite having a higher adsorption capacity than the raw material due to its higher specific surface area. In addition, the FB molecules were removed from the liquid medium by physical adsorption. Batch desorption experiments were conducted to study the desorption kinetics and the characteristics of the desorption isotherms as well as to quantify the portion of the FB (by mass) that was irreversibly fixed on the solid. Overall, the desorption kinetics were similar to the adsorption kinetics, which indicated that the adsorption-desorption process of azo dye is non-singular; irreversibility occurred that was underlined by an observed thermodynamic index of irreversibility (TII) of 0.69–0.94. The desorption isotherms of the FB depended on the mass of the FB that was initially adsorbed on the bentonite sample, suggesting hysteresis. The amount of irreversibly retained FB was between 46 and 68% of the initial adsorbed mass.

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“…Adsorption isotherms can be used to predict the design of single-stage batch adsorption systems and it is already been described by Ho and McKay [11]. Based on the best tting isotherm, a single stage adsorber as shown in Fig.…”

Section: Resultsmentioning

confidence: 99%

A Batch Adsorber Design for Rhodium Adsorption on Gallic Acid Formaldehyde Resin

Can¹,

Bulut²,

Örnek³

2015

Acta Phys. Pol. A

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The adsorption of rhodium (III) ions onto gallic acid formaldehyde resin in a batch adsorber has been studied. Adsorption experiments were carried out by agitating 1 g resin particles with 1000 ml of Rh (III) ion solution of the initial concentrations from 16.54 to 88.80 mg/l (293K, 1M HCl). Using Langmuir isotherm, a single stage batch adsorber was designed for dierent adsorbent mass/treated euent volume ratios. An initial rhodium concentration of 100 g/m 3 is assumed and the required amount of resin particles to recover metal ion content by 75%99% at various volumes of euents. For a single-stage adsorption system, thus the adsorbent demonstrated recovery capacity. For example, 1 m 3 of solution is to be treated; the required masses of gallic acid resol resin are 25 kg for 75% rhodium removal. In order to recover 90% of the rhodium (III) at various volumes of solution which having dierent metal concentrations, the required amount of gallic acid resin was calculated. For example, 1 m 3 of solution is to be treated, the required amounts of resin particles to reduce the rhodium content by 90% increased from 75 to 76 kg with increase in the initial rhodium metal concentration from 0.1 to 100 g/m 3 . Through such a projection, a real single stage adsorption system can be designed.

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Fuller's earth and fired clay as absorbents for dyestuffs external mass transport processes during adsorption

Cited by 16 publications

References 6 publications

Adsorptive removal of biophenols from olive mill wastewaters (OMW) by activated carbon: mass transfer, equilibrium and kinetic studies

Adsorptive removal of biophenols from olive mill wastewaters (OMW) by activated carbon: mass transfer, equilibrium and kinetic studies

Adsorption-desorption processes of azo dye on natural bentonite: batch experiments and modelling

A Batch Adsorber Design for Rhodium Adsorption on Gallic Acid Formaldehyde Resin

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