Kinetic, Isotherm and Thermodynamic Studies of the Adsorption of Thymol Blue onto Powdered Activated Carbons from <i>Garcinia cola Nut</i> Shells Impregnated with H₃PO₄ and KOH: Non-Linear Regression Analysis

In this work, activated carbons (ACs) prepared by chemical activation of garcinia cola nut shell impregnated with H ₃PO ₄ (CBH _2/1) and KOH (CBK _1/1) were used to study the kinetics, equilibrium and thermodynamics of the adsorption of thymol blue from aqueous solution. The characterization of ACs showed the BET measurements gave surface area and total pore volume respectively of 328.407 m ² ·g ^-1 and 0.1032 cm ³ ·g ^-1 for CBH _2/1 and 25.962 m ² ·g ^-1 and 0.03 cm ³ ·g ^-1for CBK _1/1; elemental analysis showed a high percentage of carbon in both ACs. Influence of parameters such as initial pH, contact time, adsorbent mass, initial concentration, ionic strength and the effect of temperature on the removal of thymol blue from aqueous solution were studied in batch mode. The studies showed that equilibrium adsorption was attained after 60 minutes for the two ACs, adsorption capacity increased with increasing concentration of thymol blue, and maximum adsorption capacity was obtained at an acidic environment with pH 2. Avrami’s non-linear kinetic expression was the best suited for describing the adsorption kinetics of thymol blue onto ACs, while equilibrium data showed that the three-parameter isotherms better described the adsorption process since R ² > 0.96, and the error functions were lowest for all of them. Maximum adsorption capacity values obtained using the three-parameter Fritz-Schlunder equation were 32.147 mg ·g ^-1 for CBH _2/1 and 67.494 mg ·g ^-1 for CBK _1/1. The values of the model parameters g and mFS respectively, obtained using the Redlich-Peterson and Fritz-Schlunder III isotherms below 1, showed that the adsorption of thymol blue by the ACs occurred on heterogeneous surfaces. Thermodynamic analyses of the data of the adsorption of thymol blue onto ACs revealed that the adsorption process was temperature dependent, endothermic and spontaneous.

• Garcinia Cola Nut Shell
• Chemical Activation
• Elemental Analysis
• Non-Linear Regression
• Adsorption Isotherms
• Adsorption Kinetic Models

1. Introduction

The intensive industrialization considered as key to economic development, which started in the last century is at the origin of the proliferation of various pollutants in the environment, and most of them are difficult to eliminate [1] . The wastes resulting from industrial activities represent a danger to man and his environment, due to their very low biodegradability and the slowness of their elimination [1] . The global increase in water pollution has increased awareness among the public, and more attention is being focused on combating the problem [2] .

Conventional methods are being used to remove pollutants from wastewater, some examples of which are chemical precipitation, electrodialysis, filtration, reverse osmosis, electrochemical treatment, ion exchange and adsorption onto activated carbons. In comparison with other methods, adsorption is one of the most widely used techniques for the removal of pollutant because it is cost-effective, it is simple in design and implementation and it has a high removal capacity [3] . Also, the adsorption-based treatment with suitable adsorbent material offers high performance and selectivity, and it produces little or no harmful by-products. Adsorption is widely used for removing both organic and inorganic pollutants from contaminated water [4] .

Pollutants such as pesticides, phenolic derivatives, heavy metals, and dyes have been identified as having harmful effects on humans, and they also contribute to the destruction of the environment [5] . Of these pollutants, dyes are organic compounds that are particularly dangerous to the environment [6] . About 40,000 dyes and pigments have been listed, and they consist of more than 7000 different chemical structures [7] , of which about 10,000 of them are among the various commercial dyes and pigments, and over 7 × 10⁵ tons are produced annually [8] . Dyes are used in multiple sectors of the economy, some examples of which are: in changing the colors textiles, paper, paint, cosmetics, drinks, and as food additives. Many of these dyes are carcinogenic, mutagenic, genotoxic and teratogenic and they are also toxic to human beings, fish species, and microorganisms [9] . The majority of these pollutants are not biodegradable and can constitute risk factors to our health, as well as being a nuisance to the environment. The presence of these pollutants in water, even at very low concentrations is very undesirable because it is highly visible. In fact, the presence of dyes in flowing streams causes a high reduction in the activity of photosynthesis [10] .

Thymol blue is an example of such a dye. It is used as a pH indicator in analytical chemistry. When inhaled it leads to irritation of the respiratory tract, or when it gets in contact with the skin, it is very painful [11] . These effects have become a major concern to the society. For this reason, many studies have focused on the use of depollution techniques to eliminate pollutants from wastewaters. The majority of these techniques are very expensive and difficult to implement especially when they are applied to effluents of high flow rates and having low concentrations of pollutants.

Adsorption has proved to be a more effective and cheaper process, and its equipment is easy to implement [1] . However, the choice of adsorbent remains a major worry because most adsorbent materials such as alumina, zeolites, activated clays, and silica gels are also used as catalyst support materials [12] . Therefore, activated carbons are the most commonly used adsorbents because they contain large surface areas, well-developed porosity and contains various functional groups on their surfaces.

Activated carbons prepared by chemical activation of lignocellulosic materials have been used for the adsorption of dyes, various organic compounds and antipyretic/analgesic drugs [13] [14] [15] . The advantage of chemical activation is that the pyrolysis stage of the synthesis is achieved at low temperature, thereby greatly reducing the cost of fabrication. Over the last few years, much interest has been shown by researchers on the technique of adsorption, and they have produced low cost activated carbons from lignocellulosic materials which are abundant agricultural wastes, to remove organic compounds, metals and dyes from solutions of waste streams. The costs of activated carbons prepared from lignocellulosic materials are very low compared to the cost of commercial activated carbons [9] . Many activated carbons have been produced from various carbonaceous materials resulting from agricultural wastes such as coconut shells [9] , cola nut shells [13] , rice and coffee husks [14] , Ayous sawdust and Cucurbitaceous peelings [15] , hibiscus sabdariffa and stalk biomass [16] . In this work, we will prepare ACs using shells of Garcinia cola (bitter cola) nuts [17] , due to the availability and cost free of the material as well as its high carbon content. However, little or no work has been reported on the production of activated carbons using the garcinia cola nut shells.

The aim of this work was to evaluate the adsorption properties of activated carbons prepared from garcinia cola nut shells impregnated by H₃PO₄ and KOH for the removal of thymol blue from aqueous solution. Thermodynamics studies were carried out, and the experimental data were analyzed using the two-parameter non-linear regressions kinetics, and two- to five-parameter non-linear isotherm models.

2. Materials and Methods

2.1. Chemicals: Adsorbate (Thymol Blue)

The adsorbent used in this study was thymol blue, which is an anionic dye. Thymol blue, also called thymol sulphonephthalein is a brownish-green or reddish-brown crystalline powder that is used as a pH indicator and for biological activities. It is insoluble in water, but soluble in alcohol and dilute alkali solutions. Its colour changes from red to yellow at pH 1.2 - 2.8 and from yellow to blue at pH 8.0 - 9.6. A stock of 500 mg∙L⁻¹ of thymol blue was prepared by dissolving 125 mg in 100 mL of dilute alkali solution (Na⁺ + HO⁻) using distilled water and then completing to 250 mL. Working solutions of various concentrations were freshly prepared from this stock solution. HCl or NaOH of concentration 0.1 mol∙L⁻¹ was used to adjust the initial pH of the solution. NaCl was used to study the influence of ionic strength on the adsorption process

2.2. Absorbents

The ACs used had been prepared using optimized experimental conditions by chemical activation of garcinia cola (bitter cola) nut shells. The AC CBH_2/1 was prepared by activating garcinia cola nut shells with H₃PO₄ in a ratio 2/1, while CBK_1/1 was prepared by activating with KOH in a ratio 1/1. The chemical activation was followed by calcination in a furnace set at 400˚C for 1 hour and a heating rate of 5 ˚C∙min⁻¹ as described by Idris-Hermann et al. [17] .

2.3. Characterizations

Ultimate analyses of raw material and ACs were performed for determining the C, H, N, and S content using CHNSO elemental analyses from HEKAtech CHNS Analyzer. The oxygen content was calculated by the difference on 100%. Textural analysis was performed by N₂-sorption measurements at 77 K using multipoint porosimeter automatic analyzer (Sorptomatic 1990, Porotec, GmbH), system ADP2005 Extended Report software using to calculated BET-surface area, total pore volume and pore size…, with a relative pressure range of 0.05 < P/P₀ < 0.25, with an overnight pretreatment of 150˚C for 5 hours. Total pore volume (V_tot) was estimated to be the liquid volume of N₂ at the high relative pressure P/P₀ = 0.95. The micropore volume (V_micro) was obtained using the D-R method and average pore diameter (D_P) was calculated from D_P = 4V_T/S_BET [18] . The micropore size distribution parameter was calculated according to the simplified equation of the Horvath-Kawazone (HK) [19] .

The BET specific surface area (S_BET) was calculated using the equation below:

S BET = V m ⋅ N A ⋅ σ m ⋅ V M (1)

where V_m is the volume occupied by a monolayer, N_A is the Avogadro constant 6.023 × 10²³ mol⁻¹, σ is the surface occupied by the N₂ molecule (16.2 Ų); m is the mass of the sample (g) and V_M is the molar volume of N₂ (22414 cm³∙mol⁻¹).

In our earlier work, Idris-Hermann et al. [17] , the different ACs had been characterized by proximate analysis, bulk density, pH of zero point charge (pH_zpc), methylene blue number, iodine number, surface functional groups, Fourier transform infra-red spectroscopy (FTIR), scanning electron microscopy (SEM), and power X-ray diffraction (XRD).

2.4. Batch Adsorption Experiments

Adsorption experiments were carried out by mechanical agitation at ambient temperature and constant agitation speed of 200 rpm. For each run, 20 mL of thymol blue dye solution of known initial concentration varying between 40 and 90 mg∙L⁻¹ was treated with 50 mg each of the ACs CBH_2/1 and CBK_1/1, and at pH = 2. After agitation, the solution was filtered using Whatman N˚1 filter paper and the filtrate analyzed to obtain the residual concentration of thymol blue using a UV/Vis spectrophotometer (Jenway, model 6715). Similar measurements were carried out by varying the pH of the solution, adsorbents doses, ionic strength and the initial concentration of the solution. Absorbance values were determined at a maximum wavelength (λ_max) of 435 nm. The percentage removal (%R) of dye, and the amount of dye adsorbed (Q_e) were calculated using the following expressions:

% R = C 0 − C e C 0 × 100 (2)

Q e = C 0 − C e m × V (3)

C₀ is the initial concentration of the dye, C_e is the concentration of the dye at the time t, V is the volume of the adsorbate solution, and m is the mass of the adsorbent.

2.4.1. Effect of Initial pH

To determine the effect of pH, the adsorption of thymol blue by the ACs were investigated over a pH range of 2 to 7 at ambient temperature. For each adsorbent, 50 mg was treated with 20 mL of aqueous solution of 50 mg∙L⁻¹ of thymol blue dye. The initial pH of the solution was adjusted by adding HCl or NaOH solution.

2.4.2. Effect of Contact Time

To determine the effect of agitation time on the adsorption process, 50 mg of ground adsorbent was agitated in a 20 mL solution of thymol blue of initial concentration 50 mg∙L⁻¹ for different contact times, varying between 0 and 105 minutes. After each contact time t, the solution was rapidly filtered and the residual concentration of thymol blue, C_e determined by UV/Vis spectrophotometer. The amount (Q_e) of thymol blue adsorbed was calculated using Equation (3).

2.4.3. Effect of Amount of Adsorbent

In this set of experiments, different masses of the adsorbents 30, 50, 70, 90, 110, 130, 150 and 170 mg were treated with 20 mL solution of thymol blue of initial concentration 50 mg∙L⁻¹ at the optimum time obtained from the effect of contact time experiments and the optimum pH obtained from the effect of pH experiments.

2.4.4. Effect of Ionic Strength

To determine the effect of ionic strength on the adsorption process, 50 mg of each adsorbent was agitated in a 20 mL solution of thymol blue at pH 2 of initial concentration 50 mg∙L⁻¹ containing the salt, NaCl of concentrations ranging between 0.01 and 0.06 mol∙L⁻¹. At equilibrium time (1 hour), the solution was rapidly filtered and the residual concentration of thymol blue determined by spectrophotometer. The amount (Q_e) of thymol blue adsorbed was calculated.

2.4.5. Kinetics of Adsorption Studies

To deduce the controlling mechanisms for the adsorption of thymol blue onto the ACs, data from the kinetics experiments were analyzed using the different non-linear kinetic models presented in Table 1 below.

Table 1

Non-linear forms of kinetic models

Kinetic Models	Non-Linear Forms	Equation Number	References
Pseudo-First Order:	d Q t d t = K 1 ( Q e − Q t )	(3)	[20]
	Q t = Q e ( 1 − e − K 1 t )	(4)
Pseudo-Second Order:	d Q t d t = K 2 ( Q e − Q t ) 2	(5)	[21]
	Q t = K 2 Q e 2 t 1 + K 2 Q e t and h = K 2 Q e 2	(6)
Intraparticle Diffusion:	Q t = K i n t t 1 2 + C	(7)	[22]
Elovich Model:	d Q t d t = α e − β Q t	(8)	[23]
	Q t = 1 β ln ( 1 + α β t )	(9)
Fractional Power:	Q t = K t v	(10)	[24]
Avrami:	Q t = Q e { 1 − exp [ − ( K A V t ) ] n A V }	(11)	[25]
Tobin:	Q t = Q e K T t n T 1 + K T t n T	(12)	[26]

2.4.6. Adsorption Isotherm Studies

To study the equilibrium of the adsorption of thymol blue onto the ACs, data from the equilibrium experiments were analyzed using the following two- to five-parameter, non-linear equilibrium models as presented in Table 2 below.

Table 2

Non-linear forms of two, three, four and five parameter isotherms models

Parameters	Isotherms	Non-Linear Forms	Equation Number	References
Two	Langmuir	Q e = Q m K L C e 1 + K L C e	(13)	[27]
		and R L = 1 1 + K L C 0	(14)
	Freundlich	Q e = K f C e 1 / n	(15)	[28]
	Temkin	Q e = R T Δ Q ln ( A C e )	(16)	[29]
	Dubinin-Radushkevich	Q e = Q m exp ( − β ε 2 ) Math_21#	(17)	[30]
	Elovich	Q e Q m = K E C e exp ( − Q e Q m )	(18)	[31]
	Jovanovic	Q e = Q m ( 1 − e − K J C e )	(19)	[32]
	Kiselev	K 1 k C e = θ k ( 1 − θ k ) ( 1 + K n θ k ) θ k = Q e / Q m	(20)	[3]
	Halsey	Q e = exp ( ln K H − ln C e n H )	(21)	[3]
Three	Redlich-Peterson	Q e = K R P C e 1 + A R P C e g	(22)	[3]
	Hill	Q e = Q S H C e n H K D + C e n H	(23)	[33]
	Radke-Prausnitz	Q e = Q m R P K R P C e ( 1 + K R P C e ) m R P	(24)	[3]
	Langmuir-Freundlich	Q e = Q m L F ( K L F C e ) M L F 1 + ( K L F C e ) M L F	(25)	[33]
	Toth	Q e = Q m K T C e [ 1 + ( K T C e ) n ] 1 / n	(26)	[33]
	Jossens	C e = Q e H exp ( F Q e p )	(27)	[3]
	Fritz-Schlunder III	Q e = Q m F S K F S C e 1 + Q m F S C e m F S	(28)	[9]
Four	Fritz-Schlunder IV	Q e = A C e α 1 + B C e β With α and β ≤ 1	(29)	[3] [34]
	Baudu	Q e = Q m o b o C e ( 1 + x + y ) 1 + b o C e ( 1 + x ) with ( 1 + x + y ) and ( 1 + x ) < 1	(30)	[3] [34]
Five	Fritz-Schlunder V	Q e = Q m F S K 1 C e m 1 1 + K 2 C e m 2 with m1 and m2 ≤ 1	(31)	[3] [33]

2.4.7. Non-Linear Regression Analysis

In this study, non-linear regression was applied using Microsoft Excel Solver function and using Origin Pro 9, 64 bit for fitting the curve. The best fit for experimental data was determined from the coefficient of determination (R²), residual root mean square error (RMSE), Chi-square test (χ²), Sum Square of Errors (ERRSQ), Hybrid Fractional Error Function (HYBRID), Average Relative Error (ARE), Marquardt’s Percent Standard Deviation (MPSD), Sum of Absolute Errors (EABS). More detailed definitions of the error functions and statistical comparison values are presented in Table 3.

2.4.8. Thermodynamic Studies

The effect of temperature on the adsorption of thymol blue dye onto the ACs was evaluated from thermodynamic studies. 20 mL of thymol blue solution of concentration 50 mg∙L⁻¹ (pH = 2) was placed in contact with 50 mg each of AC in a polypropylene flask and placed on a magnetic stirrer/heater and heated with stirring for the equilibrium time 1 hour, at temperatures of 35˚C, 45˚C, 55˚C and 65˚C (308, 318, 328 and 338 K). After the equilibrium time, the concentration of the remaining thymol blue was determined by spectrophotometry, and the maximum amount adsorbed calculated from Equation (3). The thermodynamic quantities, change in Gibbs free energy (∆G⁰), enthalpy change (∆H⁰) and entropy change (∆S⁰) were calculated.

Table 3

Error functions and their equations

Error Function	Abbreviation	Formula	References
Residual Root Mean Square Error	RMSE	1 n − 2 ∑ i = 1 N ( Q e , e x p − Q e , c a l ) 2	[35]
Chi-Square Test	χ2	∑ i = 1 N ( Q e , e x p − Q e , c a l ) 2 Q e , c a l	[35]
Sum Square of Errors	ERRSQ	∑ i = 1 N ( Q e , e x p − Q e , c a l ) i 2	[35]
Hybrid Fractional Error Function	HYBRID	100 N − p ∑ i = 1 N [ ( Q e , i , e x p − Q e , i , c a l ) 2 Q e , i , e x p ]	[33]
Average Relative Error	ARE	100 N ∑ i = 1 N | Q e , i , c a l − Q e , i , e x p Q e , i , e x p |	[33]
Marquardt’s Percent Standard Deviation	MPSD	100 1 N − p ∑ i = 1 N ( Q e , e x p − Q e , c a l Q e , e x p ) 2	[33]
Sum of Absolute Errors	EABS	∑ i = 1 N | Q e , e x p − Q e , c a l | i	[35]
Coefficient of Determination	R2	∑ i = 1 N ( Q e , c a l − Q m e x p ) 2 ∑ i = 1 N ( Q e , c a l − Q m e x p ) 2 + ( Q e , c a l − Q m e x p ) 2	[33]

3. Results and Discussion

3.1. Textural Characterization of the Adsorbents

Textural characteristics of all ACs were studied. As it can be observed, CBK_1/1 25.962 m²∙g⁻¹ gave the lower value of S_BET compared to CBH_2/1 328.407 m²∙g⁻¹ calculated by Equation (1). The lower porosity of CBK_1/1 is confirmed by the higher value of average pore diameter 4.622 nm, while CBH_2/1 shows D_p value of 1.257 nm smaller than 2.0 nm. However, the V_micropores of CBH_2/1 is higher than that of CBK_1/1, which corroborates the microporous characteristic of CBH_2/1. Total pore volume of CBH_2/1 0.1032 cm³∙g⁻¹ was higher than that of the CBK_1/1, of 0.03 cm³∙g⁻¹.

The values of total pore volume and BET surface area upon H₃PO₄ activation are larger because H₃PO₄ prevents the accumulation of tars on the surface of the carbon. Also, according to pore evolution theory, hydrogen and oxygen compounds in the lignocellulosic material are removed in the form of volatiles materials during decomposition. These volatiles diffuse out of the carbon matrix, leading to the development of pores.

The results obtained by scanning electron microscopy (SEM), power X-ray diffraction (XRD) had been presented in our former work, Idris-Hermann et al. [17] .

3.2. Elemental Analysis

The elemental composition (CHNS) of the raw material (CB) and the two ACs were studied and the results are presented in Table 4 below. It was obvious from the table that H₃PO₄ and KOH used as activating agents have significant influence in producing activating carbons with high ratios of C/H and C/N. As expected, the ACs have much higher contents of carbon and lower contents of oxygen and hydrogen compared to the initial raw material. As a matter of fact, the chemical activation during the heat treatment may accelerate the chemical changes in carbonaceous material and enable the removal of volatile compounds. This could be attributed to the fact that H₃PO₄ and KOH selectively stripe H and O away from the garcinia cola nutshells as H₂O and H₂ rather than CO, CO₂ or hydrocarbons [36] [37] . Therefore, the carbonaceous material becomes richer in carbon. However, elemental analyses of the activated carbons indicate the absence of sulphur for all of them.

Table 4

Elemental composition analysis

Materials	C %	H %	N %	S %	O %(diff)	Weight	C/H	C/N
CB	53.375	4.68	1.424	0	37.475	3.046	11.405	37.482
CBH2/1 400˚C	72.023	3.177	2.125	0	19.645	3.03	22.67	33.893
CBK1/1 400˚C	71.877	3.874	2.133	0	19.348	2.768	18.554	33.698

3.3. Batch Adsorption Studies

3.3.1. Effect of Initial pH

The effect of initial pH on the adsorption of thymol blue dye by the two ACs was studied by varying the initial pH of the thymol blue solution. The result is shown in Figure 1. According to this figure, the removal of dye from aqueous solution is highly dependent on the pH of the solution. In Figure 1, the results show that, the maximum capacity of adsorption is obtained at pH = 2 and favoured for pH < pH_PZC. The pH at the point of zero chage, pH_PZC was obtained for the two ACs as 7.751 for CBH_2/1 and 8.324 for CBK_1/1 [17] . When the pH increases, the capacity of adsorption decreases from 14.809 to 3.684 mg∙g⁻¹ and 15.476 to 2.514 mg∙g⁻¹ for CBH_2/1 and CBK_1/1 respectively. This can be explained by the fact that, when the pH of solution is lower than the pH_PZC, more protons will be available for protonating the surface of the ACs, thereby increasing the electrostatic attraction between the positively charged adsorbent sites and negatively charged or nucleophilic character of thymol blue. This phenomenon can also be explained by the fact that at pH = 2, the positive charge dominates on the surface of the adsorbents, hence increasing the existing electrostatic attraction between the positively charged surface of the adsorbents and negatively charged thymol blue molecules. Thymol blue dye carries a negative charge on its sulfonic ( -SO 3 − ) functional group. They are equally attracted by positively charged adsorbent site at lower pH.

However, increasing pH above pH_PZC the thymol blue becomes more soluble and the negative charges on the surface of the ACs increase the electrostatic force of repulsion between adsorbate (sulfonic functional group of thymol blue)

and –OH groups of the ACs surface due to the increased concentration of the hydroxide ions. The electrostatic force of repulsion between thymol blue and adsorbent is at the origin of the decreasing capacity of adsorption. A similar result was obtained from the adsorption of amaranth red by pineapple peelings and coconut shells¹.

3.3.2. Effect of Contact Time

The effect of contact time on the adsorption of thymol blue is given in Figure 2 below. The figure shows the evolution of the adsorption capacity of thymol blue with time of contact at ambient temperature. It can be observed that, the adsorption process took place in three phases. Rapid adsorption of thymol blue took place in the first 5 minutes for the two activated carbons. This is explained as follows: at the start of the adsorption process, all the vacant sites on the adsorbent were completely available and the thymol blue molecules were fast attached. The same tendency had been obtained by Ndifor-Angwa for and others when they adsorbed amaranth red onto treated and untreated lignocellulosic materials [1] . Thereafter, the rate of adsorption deceased gradually with the progress of adsorption within 5 to 60 minutes for the two adsorbents, and reached equilibrium in about 60 minutes. The adsorption capacity at these equilibrium points are 14.974 mg∙g⁻¹ for CBH_2/1 and 15.839 mg∙g⁻¹ for CBK_1/1. This can be explained by the fact that the available sites for adsorption have been greatly reduced by the thymol blue molecules already attached there. Also, the already adsorbed molecules tend to repel any other approaching molecules as they are similarly charged, thereby reducing the rate of adsorption. The adsorption process can be attributed to aromatic condensation due to π-π interactions between thymol

blue molecules and the surface of the adsorbent. During the aromatic condensation, it is possible that surface functional groups of adsorbent do not occupy the entire nucleophilic sites of thymol blue. Figure 2 also shows that there is no significant change in the rate of adsorption of thymol blue after equilibrium time. This corresponds to the third phase, which lies between 60 and 105 minutes, in which for CBH_2/1 and CBK_1/1 the adsorption capacities are almost constant with time.

3.3.3. Effect of Adsorbent Dosage

The effect of adsorbent dosage on the removal of thymol blue was studied and the results of this study are shown in Figure 3 below. In this figure, the percentage removal of thymol blue by CBH_2/1 and CBK_1/1 increased as the adsorbent dosage increased. The removal percentage of thymol blue increased from 63.519 to 76.623 and 66.445 to 83.058 for CBH_2/1 and CBK_1/1 respectively. This is because an increase in adsorbent mass leads to an increase in surface area, and hence an increase in the number of available adsorption sites for thymol blue to occupy during the adsorption process [38] . A similar trend was reported in Hameed et al. [39] for the adsorption of chromotrope dye onto activated carbons obtained from the seeds of various plants.

3.3.4. Effect of Initial Concentration

The effect of initial concentration on the adsorption of thymol blue was investigated and the results are show in Figure 4 below. In Figure 4, we observe that the quantity of thymol blue adsorbed at equilibrium increases from 10.519 to 34.400 mg∙g⁻¹ and 10.893 to 34.681 mg∙g⁻¹ for CBH_2/1 and CBK_1/1 respectively.

The increasing adsorption capacities of the ACs with increase in concentration of thymol blue can be due to π-π interactions between the organic compounds and functional groups of the carbon surface. The π-π interactions in most cases are responsible for the mechanism of adsorption of aromatic compounds [14] . This result can also be explained by saying that, increasing the initial concentration of thymol blue leads to an increase in the driving force for mass transfer, and hence an increase in the rate at which thymol blue molecules pass from solution to the particle surface [38] . The quantity of thymol blue adsorption onto all samples of ACs did not show a plateau, suggesting that there was no monolayer formation on the surfaces of the adsorbents. The increase in adsorption capacity with increase in initial concentration indicates that, the ACs have a high potential for the removal of thymol blue from its solutions.

3.3.5. Effect of Ionic Strength

The ionic strength can be viewed as one of the factors that controls non-electrostatic and electrostatic interactions between adsorbate and the surface of the adsorbent. The effect of ionic strength is also important in the study of adsorption of dye onto adsorbents. Ionic strength effect on the adsorption of thymol blue was investigated and the results are shown in Figure 5. In this figure, the adsorption capacities of dye at equilibrium decreased from 13.347 to 12.072 mg∙g⁻¹ for CBH_2/1 and 13.336 to 12.271 mg∙g⁻¹ for CBK_1/1 when the ionic strength increased from 0.01 to 0.06 mol∙L⁻¹. These results can be explained by the fact that, the surface of ACs becomes less accessible to thymol blue molecules when the quantity of NaCl salt in solution increases. For this reason, the amount of thymol blue adsorbed decreases. This result is in agreement with the literature,

which reports that when the electrostatic attraction forces between the adsorbent surface and adsorbate ions are attractive, an increase in ionic strength will decrease the adsorption capacity [40] .

3.4. Batch Kinetic Studies

Pseudo-first order, pseudo-second order, intraparticle diffusion, Elovich, fractional power, Avrami and Tobin kinetics models are used to investigate and describe the mechanism of the adsorption process (see equation in Table 1). These kinetic models have been presented in different non-linear forms and Table 5 presents the calculated parameters.

According to Table 5, the non-linear models of pseudo-second order, Avrami and Tobin seem to be the most appropriate in adequately describing the adsorption phenomenon for the two ACs, CBH_2/1 and CBK_1/1 studied. As shown in Table 6, the coefficient of determination, R² of these models are very good (R² > 0.95). However, the relatively higher R² values and the lower χ², ERRSQ values and other relatively lower error functions for the Avrami model compared to the pseudo-second order and Tobinmodels confirm that the Avrami non-linear kinetic expression is best suited to describe the adsorption kinetics of thymol blue on the two ACs. The Avrami exponent (n_AV) is a fractional number that is related to the possible changes in the adsorption mechanism that takes place during the adsorption process [41] . Therefore, instead of following only an integer-kinetic order, the adsorption mechanism could follow multiple kinetic orders. That is, during adsorption, the order of reaction can change from one value to another [41] . In this study, n_AV exponent showed that the adsorption process was of the multiple kinetic order. The low values of χ² and other error functions

Table 5

Kinetic data obtained by non-linear fitting analysis (see equations in Table 1 and Table 3 )

Models	Constants	Values	R2	χ2	RMSE	ERRSQ	HYBRID	ARE	MPSD	EABS
CBH2/1
Pseudo-First Order	Qe (mg∙g−1)	14.387	0.922	0.276	0.608	2.956	3.311	3.786	5.534	4.548
	K1 (min−1)	0.170
Pseudo-Second Order	Qe (mg∙g−1)	15.464	0.963	0.087	0.378	1.141	1.097	2.273	2.933	2.999
	K2 (g∙mg−1∙min−1) h (mg∙g−1∙min−1)	0.0191 4.567
Intra-Particle Diffusion	C (mg∙g−1)	9.834	0.681	0.781	1.113	9.909	10.461	7.209	9.6	9.016
	Kid (mg∙g−1∙min−0.5)	0.593
Elovich	α (mg∙g−1∙min−1)	113.57	0.851	0.359	0.761	4.635	4.565	4.808	6.101	6.155
	β (g∙mg−1)	0.564
Fractional Power	K	8.576	0.803	0.464	0.858	5.885	6.018	5.52	7.156	6.971
	V	0.130
Avrami	Qe (mg∙g−1)	14.771	0.974	0.063	0.318	0.811	0.802	2.035	2.548	2.624
	KAv (min−1) nAv	0.187 0.642
Tobin	Qe (mg∙g−1)	15.255	0.965	0.085	0.369	1.091	1.085	2.282	2.972	2.939
	KT nT	0.249 1.103
CBK1/1
Pseudo-First Order	Qe (mg∙g−1)	22.838	0.755	0.301	0.701	3.927	3.935	4.184	5.708	5.518
	K1 (min−1)	0.068
Pseudo-Second Order	Qe (mg∙g−1)	16.075	0.951	0.107	0.426	1.451	1.342	2.494	3.184	3.396
	K2 (g∙mg−1∙min−1) h (mg∙g−1∙min−1)	0.02 5.168
Intra-Particle Diffusion	C (mg∙g−1)	10.591	0.702	0.641	1.045	8.742	8.376	6.246	8.141	8.414
	Kid (mg∙g−1∙min−0.5)	0.585
Elovich	α (mg∙g−1∙min−1)	197.388	0.862	0.288	0.711	4.039	3.621	4.056	5.152	5.605
	β (g∙mg−1)	0.576
Fractional Power	K	9.296	0.822	0.367	0.794	5.042	4.659	4.656	5.950	6.352
	V	0.121
Avrami	Qe (mg∙g−1)	15.576	0.961	0.084	0.379	1.146	1.044	2.129	2.785	2.909
	KAv (min−1) nAv	0.213 0.562
Tobin	Qe (mg∙g−1)	16.188	0.951	0.105	0.424	1.440	1.311	2.441	3.123	3.355
	KT nT	0.354 0.952

Table 6

Adsorption of thymol blue: non-linear fitting analysis for two-parameter isotherms (see Equations in Table 2 and Table 3 )

Models	Constants	Values	R2	χ2	RMSE	ERRSQ	HYBRID	ARE	MPSD	EABS
CBH2/1
Langmuir	Qm (mg∙g−1)	396.04	0.989	0.094	0.730	2.132	2.388	2.191	3.403	2.819
	KL (L∙mg−1)	0.0071
Freundlich	KF (L∙g−1)	2.645	0.994	0.076	0.589	1.392	1.871	2.215	3.303	2.605
	1/n	1.000
Jovanovic	Qm (mg∙g−1)	188.68	0.989	0.099	0.753	2.269	2.530	2.233	3.490	2.901
	KJ (L∙mg−1)	0.015
Temkin	∆Q (J∙mol−1)	120.86	0.962	0.413	1.410	7.957	10.006	5.158	7.438	6.157
	A (L∙g−1)	0.367
Halsey	KH	0.378	0.994	0.076	0.590	1.392	1.870	2.215	3.301	2.604
	nH	−0.999
D-R	Qm (mg∙g−1)	36.892	0.924	0.965	2.081	17.314	22.27	7.714	11.234	9.149
	β (mol2∙kJ−2)	5.708
Elovich	Qm (mg∙g−1)	445.50	0.989	0.096	0.733	2.151	2.432	2.242	3.455	2.850
	KE (L∙mg−1)	0.0063
Kiselev	K1K (L∙mg−1)	0.014	0.994	0.083	0.590	1.393	2.000	2.273	3.510	2.606
	Kn	−0.674
CBK1/1
Langmuir	Qm (mg∙g−1)	189.6	0.992	0.102	0.666	1.774	2.471	3.394	3.822	2.657
	KL (L∙mg−1)	0.019
Freundlich	KF (L∙g−1)	4.019	0.994	0.066	0.555	1.232	1.639	1.941	3.048	2.337
	1/n	0.871
Jovanovic	Qm (mg∙g−1)	195.51	0.990	0.189	0.807	2.606	4.310	2.684	5.377	2.686
	KJ (L∙mg−1)	0.017
Temkin	∆Q (J∙mol−1)	127.73	0.963	0.560	1.500	9.002	12.710	5.234	8.751	6.058
	A (L∙g−1)	0.459
Halsey	KH	0.202	0.994	0.066	0.555	1.232	1.639	1.941	3.048	2.337
	nH	−1.148
D-R	Qm (mg∙g−1)	35.11	0.909	1.071	2.284	20.866	25.314	8.211	11.584	10.214
	β (mol2∙kJ−2)	3.648
Elovich	Qm (mg∙g−1)	260.73	0.990	0.165	0.770	2.373	3.801	2.652	4.996	2.783
	KE (L∙mg−1)	0.013
Kiselev	K1K (L∙mg−1)	0.018	0.990	0.129	0.736	2.167	3.109	2.496	4.339	2.872

of the Tobin and pseudo-second order models suggest that these two models equally describe the kinetics of thymol blue uptake onto the ACs. The values of V lower than unity obtained for the fractional power kinetic model suggest that fractional power may also describe the adsorption kinetics of the thymol blue-AC system. Adsorption data obtained from the pseudo-second order kinetic model thus indicate that the adsorption of thymol blue onto the ACs CBH_2/1 and CBK_1/1 may also be of a chemical nature.

3.5. Adsorption Isotherms

Adsorption isotherms describe the relationship between the quantity of adsorbate adsorbed by the adsorbent (Q_e) and the concentration of adsorbate remaining at equilibrium (C_e). This part aims at finding the models that can accurately describe the data obtained from the experiments of the adsorption thymol blue onto CBH_2/1 and CBK_1/1, and then to specify the parameters that can be determined. Eight models of two-parameter isotherms, seven models of three-parameter isotherms, two models of four-parameter isotherms and one model of five-parameter isotherms were studied (see equation in Table 2).

3.5.1. Two Parameter Models

The capabilities of the equations of the two-parameter isotherms to model equilibrium adsorption data were examined and Table 6 also presents the calculated parameters of the adsorption isotherms and their characterizations obtained using the non-linear model analysis.

It can be observed from the table that for the two ACs, the coefficient of determination for all the models is very good (R² > 0.96) except for the Dubinin-Radushkevich model. Thus, in this table the lower values of chi-square (χ²), RMSE, ERRSQ, ARE and other error functions for each isotherm model will determine the best model. Among the two-parameter equations tested, and based on the low values of the error functions and the high determination coefficient, the best representation of the experimental data of the adsorption of thymol blue is obtained using the isotherms of Freundlich, Halsey and Kiselev for CBH_2/1; and those of Freundlich, Halsey and Langmuir for CBK_1/1. In this table, the Halsey adsorption isotherm confirms the multilayer adsorption and the heteroporous nature of the adsorbents. The values of 1/n for the Freundlich model are equal and lower than 1 (1.000 for CBH_2/1 and 0.871 for CBK_1/1), thereby indicating the high affinity between these ACs and thymol blue solution. This also indicates that adsorption took place through a physical process, and that there was a greater heterogeneity of the adsorption sites on the adsorbent. The 1/n = 1 for CBH_2/1 indicates that the isotherm is linear, and is of the type C, while for CBK_1/1, the value of 1/n < 1 indicates the isotherm to be concave, and hence of type L.

For CBH_2/1 the negative value of k_n for the Kiselev isotherm shows that there is no complex formed between the adsorbed thymol blue molecules and the AC. On the other hand, the positive value of k_n with CBK_1/1 shows the formation of a complex between the adsorbed thymol blue molecules and the AC. The Jovanovic isotherm describes an approximation of a monolayer localized adsorption without lateral interactions. The results of the Temkin model show that the change in the adsorption energy for the two ACs is higher than zero, thus indicating that the process of adsorption is exothermic.

For the Langmuir isotherm, the values of the separation factor falling between 0 - 1 (Figure 6) show a favorable adsorption of thymol blue by the two ACs. This result is in agreement with what was already observed with the Freundlich isotherm.

3.5.2. Three Parameter Models

The capabilities of the equations of the three-parameter isotherms to model equilibrium adsorption data were examined. Table 7 presents the calculated parameters of the adsorption isotherms and their characterizations obtained using the non-linear model analysis.

It can be observed in Table 8 that for the two ACs, the coefficient of determination for all models is very good (R² > the 0.96). Thus, in this table, the lower values of the chi-square (χ²), RMSE, ERRSQ, ARE and other error functions for each isotherm model and high value of determination coefficient will determine the best model. According to these values, the best-fitted adsorption isotherm models were found in the order: Fritz-Schlunder III > Redlich-peterson > Radke-Prausnitz > Jossens > Toth > Langmuir-Freundlich > Hill for CBH_2/1 predicting the adsorption to be on heterogeneous surfaces; Fritz-Schlunder III > Redlich-peterson > Radke-Prausnitz > Hill > Langmuir-Freundlich > Jossens > Toth for CBK_1/1 predicting the adsorption process as a cooperative phenomenon

Table 7

Adsorption of thymol blue: Non-linear fitting analysis for three-parameter isotherms (see Equations in Table 2 and Table 3 )

Models	Constants	Values	R2	χ2	RMSE	ERRSQ	HYBRID	ARE	MPSD	EABS
CBH2/1
Redlich-Peterson	KRP (L∙g−1)	2.898	0.993	0.075	0.590	1.393	2.478	2.206	3.788	2.599
	ARP (L∙mg−1)	0.091
	g	0.0099
Hill	QSH (mg∙g−1)	198.96	0.990	0.115	0.737	2.170	3.746	2.547	4.628	3.018
	KD	61.164
	nH	1.198
Radke-Prausnitz	QmRP (mg∙g−1)	60.903	0.994	0.076	0.590	1.393	2.484	2.209	3.797	2.602
	KRP (L∙mg−1)	0.043
	mRP	0.001
Langmuir-Freundlich	QmLF (mg∙g−1)	173.79	0.991	0.104	0.692	1.916	3.383	2.470	4.437	2.908
	mLF	1.144
	KLF	0.022
Toth	QmT (mg∙g−1)	81.080	0.991	0.087	0.686	1.885	2.898	2.196	3.852	2.719
	n	2.721
	KT	0.033
Jossens	H	2.670	0.994	0.0755	0.590	1.394	2.484	2.209	3.796	2.602
	F	0.0063
	p	0.0508
Fritz-Schlunder	QmFS (mg∙g−1)	32.147	0.994	0.075	0.590	1.392	2.477	2.205	3.786	2.599
	KFS (L∙mg−1)	2.739
	mFS	0.0009
CBK1/1
Redlich-Peterson	KRP (L∙g−1)	10.688	0.9942	0.068	0.562	1.264	2.253	1.963	2.531	2.359
	ARP (L∙mg−1)	1.698
	g	0.181
Hill	QSH (mg∙g−1)	196.92	0.992	0.097	0.6597	1.741	3.151	2.264	4.285	2.720
	KD	54.67
	nH	0.988
Radke-Prausnitz	QmRP (mg∙g−1)	68.317	0.992	0.096	0.648	1.681	3.115	2.213	4.287	2.602
	KRP (L∙mg−1)	0.052
	mRP	0.438
Langmuir-Freundlich	QmLF (mg∙g−1)	174.40	0.992	0.098	0.671	1.802	3.200	2.338	4.264	2.803
	mLF	1.002
	KLF	0.0206
Toth	QmT (mg∙g−1)	85.551	0.991	0.128	0.730	2.130	4.083	2.467	4.983	2.838
	n	1.677
	KT	0.039
Jossens	H	3.955	0.992	0.111	0.686	1.883	3.570	2.309	4.629	2.677
	F	0.044
	p	0.543
Fritz-Schlunder	QmFS (mg∙g−1)	67.494	0.994	0.066	0.555	1.233	2.188	1.941	3.522	2.337
	KFS (L∙mg−1)	4.077
	mFS	0.131

Table 8

Adsorption of thymol blue: Non-linear fitting analysis of four- and five-parameter isotherms (see Equations in Table 2 and Table 3 )

Four Parameter Models
Models	Constants	Values	R2	χ2	RMSE	ERRSQ	HYBRID	ARE	MPSD	EABS
CBH2/1
Baudu	Qm0 (mg∙g−1)	66.513	0.993	0.087	0.633	1.603	4.274	2.318	4.993	2.724
	b0	0.038
	x	−0.299
	y	0.398
Fritz-Schlunder	A (L∙g−1)	4.628	0.994	0.076	0.590	1.393	3.743	2.216	4.670	2.605
	B (L∙mg−1)	0.750
	α	1.011
	β	0.024
CBK1/1
Baudu	Qm0 (mg∙g−1)	84.334	0.994	0.067	0.575	1.323	3.338	2.037	4.230	2.504
	b0	0.0501
	x	−0.608
	y	0.508
Fritz-Schlunder	A (L∙g−1)	5.659	0.9943	0.066	0.555	1.234	3.281	1.941	4.312	2.337
	B (L∙mg−1)	0.408
	α	0.877
	β	0.0225
Five parameter models
Models	constants	values	R2	χ²	RMSE	ERRSQ	HYBRID	ARE	MPSD	EABS
CBH2/1
Fritz-Schlunder	QmFS (mg∙g−1)	25.553	0.994	0.076	0.590	1.392	7.486	2.216	6.606	2.604
	K1	0.163
	K2	0.575
	m1	1.00
	m2	0.008
CBK1/1
Fritz-Schlunder	QmFS (mg∙g−1)	31.087	0.9943	0.066	0.555	1.232	6.559	1.941	6.097	2.337
	K1	0.196
	K2	0.514
	m1	0.874
	m2	0.008

with adsorbates at one site of the adsorbent influencing different binding sites on the same adsorbent on heterogeneous surfaces. The maximum adsorption capacity obtained using the Fritz-Schlunder III equation is 32.147 mg∙g⁻¹ for CBH_2/1 and 67.494 mg∙g⁻¹ for CBK_1/1. The values of g and m_FS obtained using Redlich-Peterson and Fritz-Schlunder III isotherms are lower than 1, which means that the adsorption of thymol blue by the ACs cannot be reduced to the Langmuir isotherm. This implies that the adsorption already predicted to be on heterogeneous surfaces is also confirmed by the Jossens model. For the two ACs, it was observed that n was greater than unity. This suggests that the interactions between the adsorbed molecules are stronger than the adsorptive potential.

3.5.3. Four and Five Parameter Models

Isotherms of four-parameters (Fritz-Schlunder IV and Baudu) and five-parameters (Fritz-Schlunder V) were used to model the equilibrium data of adsorption of thymol blue and Table 8 presents the calculated parameters of the adsorption isotherms and their characterizations obtained using non-linear model analysis.

It can be observed from Table 8 that the coefficients of determination for all models are very good (R² > 0.99). Based on the low values of ERRSQ and other error functions, high coefficients of determination, the two four-parameter isotherms gave a good fitting of the experimental results for both CBH_2/1 and CBK_1/1. The maximum adsorption capacity obtained using the Baudu isotherm were higher than those calculated by the Fritz-Schlunder-III model. However, according to Fritz-Schlunder-III and Baudu isotherm models, CBK_1/1 gave a higher maximum adsorption capacity than CBH_2/1. Examining the exponent values in the Fritz-Schlunder-IV model, α approached unity while β did not, indicating that the adsorption data could not preferably be fitted with the Langmuir isotherm.

The adsorption data were analyzed according to the non-linear form of the five-parameter isotherm model of Fritz-Schlunder-V and a satisfactory fitting of the experimental result was obtained, using the high values of the coefficient of determination and the lower values of error functions according to table 8 below. From the results obtained we can say that this model also describes the adsorption of thymol blue on CBK_1/1 and CBH_2/1. The model exponents of the Fritz-Schlunder-V isotherm, m₁ (1.00 for CBH_2/1; 0.874 for CBK_1/1) close to unity and m₂ (0.008 for CBH_2/1 and CBK_1/1) very far away from unity, show that the adsorption data did not follow the hypotheses of the Langmuir isotherm.

Comparing the selected isotherm models used, we can say from the values of the determination coefficient and the values of error functions, that the models with 3, 4 and 5 parameters better described the adsorption process than the models with 2 parameters for the two ACs.

3.6. Effect of Temperature and Thermodynamic Study

The results of the effect of temperature on the adsorption of thymol blue are shown in Figure 7 below. The adsorption of thymol blue appears to be significantly affected by the temperature which influences the quantity adsorbed. We found that as the temperature increased from 35˚C to 65˚C, the adsorption capacity also increased from 15.08 mg∙g⁻¹ to 18.062 mg∙g⁻¹ for CBH_2/1 and 15.711 mg∙g⁻¹ to 18.659 mg∙g⁻¹ for CBK_1/1. Hence, a change in temperature has an impact on the adsorption efficiency and the adsorption capacity of the adsorbent.

Higher temperatures could also lead to stronger interactions during the formation of intermolecular hydrogen bonding between thymol blue and the two ACs, which is an important contribution to the adsorption process. Also, the rise in solution temperature increased the surface activity and kinetic energy of the thymol blue molecules which in turn increased mass transfer across the liquid film surrounding the different particles of the activated carbons.

The thermodynamic behavior for the adsorption on the two ACs was studied in more detail. The thermodynamic parameters such as the changes in Gibbs free energy (∆G°), enthalpy (∆H°), and entropy (∆S°) were calculated using the following equations:

Δ G ° = Δ H ° − T Δ S ° (32)

ln K D = − Δ H ° R T + Δ S ° R (33)

where,

K D = Q e C e (34)

K_D is the distribution coefficient for adsorption, Q_e is the adsorption capacity at different temperature (mg∙g⁻¹) and C_e is the equilibrium dye concentration in solution (mg∙L⁻¹), R is the gas constant (8.314 J∙mol⁻¹∙K⁻¹), and T is absolute temperature (K). The Van’t Hoff Equation (33) was plotted and the plot was used to calculate the change in enthalpy (∆H°) and entropy (∆S°) of adsorption for the adsorption of thymol blue. The results were used to determine the change in Gibbs free energy (32). These thermodynamic quantities are presented in Table 9 below.

Table 9

Thermodynamic parameters for the adsorption of thymol blue onto the three ACs

∆G° (kJ∙mol−1)					∆H° (kJ∙mol−1)	∆S° (J∙mol−1∙K−1)
ACs	308 K	318 K	328 K	338 K
CBH2/1	−0.582	−1.642	−2.702	−3.762	32.059	105.978
CBK1/1	−1.092	−2.381	−3.671	−4.96	38.612	128.91

The negative values of ∆G° for the temperature range 308 K to 338 K indicate that the adsorption of thymol blue onto the ACs is a spontaneous process. The decrease of ∆G° values with the increase of temperature indicates that the adsorption became less favorable at higher temperatures [42] . The positive values of ∆H° show that the adsorption process is endothermic. The change in entropy (∆S°) was positive, indicating that the entropy of the system increased during the adsorption process. However, it should also be noted that the entropy of the universe (including the system and the surroundings) might increase because the adsorption process was not an isolated one [9] . A positive value of ∆S° reflects the affinity of the adsorbent towards the adsorbate species.

4. Conclusions

The ACs prepared from garcinia cola nut shell were characterized to obtain their physic-chemical properties. They were used to adsorb thymol blue from aqueous solution by batch process. Textural characteristics obtained by N₂ adsorption-desorption analysis showed that the surfaces of the ACs were heterogeneous, and contained micropores and mesopores.

Batch adsorption studies showed that increasing initial dye concentration enhanced the interaction between thymol blue and ACs which resulted in the increase of adsorption capacity. Electrostatic attraction and π-π interactions were shown to dominate the adsorption mechanism. The quantity of thymol blue adsorbed increased with increasing temperature. According to seven different error functions and coefficient of determination, kinetic studies shows that, the adsorption data best fitted the Avrami non-linear equation and the pseudo-second order kinetic model thus indicating that the adsorption of thymol blue on the ACs may also be of a chemical nature. Isotherms models confirmed that the system is heterogeneous in nature and the adsorption is of a physical nature.

In future studies, we plan to use these activated carbons for the purification of biogas by adsorption of the H₂S contained in the synthesized mixture. We also intend to use the activated carbons in studies of column adsorption.

Acknowledgements

The authors are grateful for technical assistance rendered by Doungmo Giscard of the Institute of Inorganic Chemistry, Christian-Albrechts-Universität zu Kiel, Max-Eyth-Straβe 2, 24118 Kiel, Germany, the World Academy of Sciences and the researchers of Materials and Process Engineering Team/RU-NOGEE of the Department of Chemistry, Faculty of Science of the University of Dschang, Cameroon.

Conflicts of Interest

Authors have declared a no competing interests regarding the publication of this paper.

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