Adsorptive removal of malachite green dye from aqueous solution onto activated carbon of Catha edulis stem as a low cost bio-adsorbent

The release of hazardous synthetic dyes into industrial effluents has emerged as an environmental problem requiring remediation. The present study focused on the preparation of a new and environmentally-friendly material (adsorbent) for the remediation of hazardous dyes from aqueous solution. The low cost adsorbent was prepared from locally available khat (Catha edulis) stem which considered as waste and accumulated on waste disposal areas of Woldia town, Ethiopia. Comprehensive characterization studies were carried out on the bio-adsorbent such as proximate analyses, specific surface area, point of zero charge and FT-IR analysis. The proximate analysis shows the prepared adsorbent has very high fixed carbon content (83.65%), which refers to high quality of the adsorbent. The adsorption performance of the prepared activated carbon was optimized by varying operational parameters such as initial dye concentration (10 mg/L), pH (10), dosage (0.5 g), and contact time (60 min). The maximum removal efficiency of the prepared adsorbent at those optimum conditions was 98.8%. The experimental data was tested by most common kinetics and isotherm models. It was observed that the pseudo-second-order kinetic model fits better with good correlation coefficient and the equilibrium data fitted well with the Freundlich isotherm model. In summery this study demonstrated that the waste bio sorbent could be employed as an effective and eco-friendly alternative for the cleanup of dye-polluted aqueous system.


Background
One of the major problems faced by many countries around the world is the increase in industrial activities releases effluents containing pollutants such as heavy metal ions, organic dyes and pharmaceuticals into the aquatic environment, which cause significant health hazards to living organisms and overall deterioration of the environment (Deng et al. 2011;Munagapati et al. 2018;Nhung et al. 2018). Among different industrial pollutants colored materials and dyes constitute the focus of many environmental concerns because of their non-biodegradable and polluting nature (Ai et al. 2011;Bello et al. 2010;Georgin et al. 2018;Mall et al. 2005). The source of these dyes are different dye manufacturing and processing industries such as textile, paper, plastics, cosmetics, leather and food as they use dyes for coloring their products (Ai et al. 2011). Among the various industrial dyes malachite green (MG), tri-phenyl methane water soluble cationic dye, has been widely used for the dyeing of leather, wool and silk, paper, as well as in distilleries (Dos Reis et al. 2011). In addition, MG is also used as a fungicide, tropical anti-protozoal agent, and antiseptic in the aquaculture industry to control fish parasites and disease (Georgin et al. 2018;Raval et al. 2016;Yakout and Shaker 2016). However, MG is very dangerous and highly cytotoxic to mammalian cells; it also acts as a liver tumour-enhancing agent, carcinogenic, mutagenic and teratogenic effects on human health and biota (Yakout and Shaker 2016;Zhang et al. 2014).
About 50% of the total world production of dyes goes off during the dying process and have been release in textile effluents (Sharma et al. 2010). Also, the presence of very small amounts of dyes in water < 1 ppm for some dyes is highly visible, very difficult to biodegrade, extremely difficult to eliminate in natural aquatic environments and undesirable. Moreover, most of these dyes can cause allergy, dermatitis, skin irritation and also provoke cancer and mutation in humans (Ghaedi et al. 2015;Regti et al. 2017). Hence, their removal from industrial effluents before discharge into the environment is extremely important. A number of technologies have been applied over the years for the treatment of dyecontaining wastewaters such as flocculation membrane filtration, precipitation, electrochemical, and adsorption can be used successfully for the removal of different dyes and pigments from aqueous phase (Asfaram et al. 2014;Silveira et al. 2014). Each technique has its own advantages and drawbacks. The literature indicates that nowadays, those dye removal techniques and investigations are dominant through adsorption technology (Fito et al. 2019;Mezohegyi et al. 2012). The use of wasted martial as adsorbents has received especial interest from several researchers for different reasons such as high selectivity, low cost, availability, and efficiency (Giwa et al. 2013;Mezohegyi et al. 2012). According to different scholar findings the following martials were used for removal of dyes such as: agricultural wastes (Kadirvelu et al. 2003), magnetite loaded multi-wall carbon nanotube (Ai et al. 2011), treated avocado shells (Georgin et al. 2018), Brazilian pine-fruit shell (Royer et al. 2009), spent coffee (Safarik et al. 2012), montmorillonite clay (Almeida et al. 2009), Fe 3 O 4 nanoparticle (Ghaedi et al. 2015), activated carbon, graphene oxide, and carbon nanotubes (Li et al. 2013), palm oil mill effluent waste (Gobi et al. 2011), Bagasse Fly Ash (Gupta et al. 2000), tree fern (Ho et al. 2005) etc. Various new materials with interesting adsorption capacities that can be used on sorption processes are discovered every year.
In Ethiopia one of the major problems in cities is the use of Catha edulis leaves for stimulating purpose and discarding unusable part. Khat or in its scientific name Catha edulis, is a dicotyledonous evergreen shrub of the family Celastraceae (Kennedy 1987). The oral traditions claim that Catha edulis originated from Yemen; however the literature indicates that Catha edulis originated from Ethiopia, specifically in Hararghe with a gradual expansion to different parts of Ethiopia, Yemen and other parts of the world. Studies on the chemical composition of the extracts of Catha edulis leaves identified as different compound under the group of alkaloids, terpenoids, flavonoids, sterols, glycosides, tannins, amino acids, vitamins, and minerals (Nigatu and Libsu 2019). Catha edulis consumers mostly use only the tip fleshy leaf part of the plant and throw the stems away which is considered as a waste and get disposed of everywhere especially around the Khat market areas, streets, and dumpsters area in Woldia town, Ethiopia. The present study focused on the development activated carbon from khat (Catha edulis) stem by physical and chemical activation process for removal of basic cationic dye (malachite green dye) from aqueous solutions.

Chemicals used
MG dye powder was taken from Woldia University, chemistry department laboratory and other reagents used in this work were purchased from sigma Aldrich. All the chemicals were analytical reagent grade and used as such without further purification. Malachite green oxalate [CI = 42,000, CAS number = 123333-61-9, λ max = 618 nm] has a chemical formula of C 52 H 54 N 4 O 12 with molecular weight of 927.00 g/mol. The chemical structure of MG dye is presented in Scheme 1 below.
Deionized and distilled water were used to prepare all solutions. The MG stock solution was prepared by dissolving an accurately weighed quantity of dye in deionized water and was subsequently diluted to the required concentrations. The maximum wave length was determined by scanning a known concentration of dye from 200 to 800 nm using UV-vis spectroscopy.

Adsorbent preparation
Sample preparation was conducted according to (Fito et al. 2019;Ghaedi et al. 2012Ghaedi et al. , 2014Regti et al. 2017) with little modifications and presented on Fig. 1 in short summary. Khat (Catha edulis) stem samples used for the preparation of activated carbon were collected from dumping sites "Khat terra" of Woldia town, N OOCCOOH 2 (COOH) 2 N Scheme 1. The chemical structure of malachite green Ethiopia. The sample was washed with distilled water to remove dust and any other water soluble impurities in the sample. Then the stem exposed to sunlight for several dyes and then oven dried at 105 °C until completely dried and cut into pieces at the size of 10 mm. The dried material was then milled by ball miller and separated by manually shaking stainless steel mesh screens with the opening of standard 1 mm sieve size. The sieved raw material was physically activated by carbonization in a muffle furnace (Nabertherm B180) for 2 h at 400 °C in the absence of air by placing the sample in a well-sealed stainless steel tube. Then the sample was allowed to cool for a few minute and it ready for chemical activation. The chemical activation was carried out by taking appropriate weight of powdered sample and immersed in 1 N of NaOH with a mass ratio (1:5 w/v) for 12 h. The soaked sample was filtered by Whatman filter paper and washed with 2 N of HCl several times and then with distilled water until the pH reached to neutral. The resulting activated carbon was completely dried at 110 °C in an oven for 3 h in order to achieve good carbon structure and a large surface area and kept in desiccators for further study.

Characterization of prepared adsorbent
The physicochemical properties of the adsorbent such as moisture content, ash content, volatile matter, and fixed carbon were determined according to Fito et al. 2019;Temesgen et al. 2018) with slight modifications. The thermal drying method was applied for the proximate analysis of the adsorbent.

Moisture content
The adsorbent sample of 1.0 g was weighed in triplicate and placed in a clean, dried, and weighed crucible in a preheated oven at 110 °C. The crucibles with samples were placed in an oven at 110 °C for 2 h. Then, the sample was cooled in desiccators at ambient temperature and its weight was measured again. Hence, the difference between the initial (M 0 ) and the final mass (M 1 ) of the CAC was used to determine the moisture content using Eq. 1.

Ash content
About 1 g of adsorbent sample was placed in crucibles, weighted and heated in a muffle furnace (Nabertherm B180) under a temperature of 500 °C for 4 h. After that, the crucibles containing sample was allowed to cool in a desiccator to room temperature and reweighed. The ash content of sample was calculated using the Eq. 2.
where M a and M s are the mass (g) of the adsorbent and ash, respectively.

Volatile mater
For the determination of the volatile matter of the adsorbent, 1.0 g of the activated carbon sample was taken and placed in a pre-dried crucible and heated in a muffle furnace regulated at 800 °C for 8 min. Ten, the crucible was cooled in desiccators and weighed. Finally, the volatile matter of the activated carbon was calculated using Eq. 3.
where M 1 and M 2 are initial mass (g) of adsorbents and final mass (after drying), respectively.

Fixed carbon content
It was determined by deducting the moisture, volatile, and ash content percentage from 100% using the Eq. 4.

Surface area determination
The specific surface area of the adsorbent was estimated according to sear method (Ahmad et al. 2013;Jawad et al. 2019). About 1.5 g prepared adsorbent was mixed with 30 g NaCl and dissolved by 100 mL of distilled water using 250 mL conical flask. The mixtures were stirred for 5 min. Then, the pH of solution was adjusted to 4, and the solution was titrated by 0.1 M NaOH until pH of the solution reaches to 9. The volumes of NaOH required to change pH value from 4 to 9 were recorded. The specific surface area of sample was obtained using the following formula: where V is the volume of 0.1 M NaOH required to raise the pH from 4.0 to 9.0. The pH point of zero charge (4) Fixed carbon content (FC)% = 100% − (MC + AC + VM)%.

Fourier transforms infrared spectroscopy (FT-IR) characterization
The surface functional group of the prepared activated carbon was estimated by using FTIR spectroscopy (JASCO model 4100). The sample was mixed with dry KBr in the ratio of 2:200 in mg and ground very well. The adsorbent sample was scanned over a wavelength range of 400-4000 cm −1 using FTIR spectrophotometry.

Batch adsorption experiments
The adsorption experiments were carried out according to (Dos Reis et al. 2011;Ghaedi et al. 2014;Li et al. 2013Li et al. , 2019 with slight modifications. The influences of experimental parameters of initial dye concentration (10-50 mg/L, step size: 10 mg/L) and pH (2-12, step size: 2) and adsorbent dose (0.2-1.4 g, step size: 0.3 g, string speed 400 rpm and at room temperature (25 °C) on the removal of MG were studied in a batch mode of operation. A measure amount of known concentration dye sample (50 mL) and 0.5 g adsorbent was taken in 250 mL of conical flask and the desired solutions pH was adjusted with 0.1 M HCl or 0.1 M NaOH for batch experiment. The mixed solutions agitated with magnetic stirrer on digital hot plate at 400 rpm until the required time reached and then the adsorbent was separated from solution by centrifugation at 4000 rpm for 10 min. The absorbance of remain supernatants solutions were determined by using UV-Vis spectrophotometer at a maximum wave length of 618 nm. The equilibrium adsorption capacity, q e (mg/g) and removal efficiency were calculated by Eqs. 6 and 7 as follows: where C 0 is the initial dye concentration (mg/L); C e is the residual concentrations of the dye (mg/L) at equilibrium; V is the volume of the dye solution (L); m is the mass of the adsorbents (g). Kinetic studies were also followed according to the method described in batch equilibrium method above. The adsorption capacity q t (mg/g) at different contact time t (min) was determined using the following equation: where C 0 , C e , and C t (mg/L) are MB solution concentrations at initial, equilibrium, and time t (min), respectively. In order to determine the maximum adsorption capacity, the amount of MG adsorbed by activated carbon of Catha edulis based on initial MG concentration was applied to Freundlich and Langmuir isotherms.

Characterization of activated carbon Proximate analysis results
The physicochemical properties of Catha edulis activated carbon was determined by standard method and presented in Table 1 below. The result showed that the prepared activated carbon has very high fixed carbon content (83.65%), very low moisture content (5.38%), very low ash content (6.72%) and very low volatile matter (4.25%). This is due to carbonization and activation processes, organic substances become unstable as a result of the heat causing the molecules to break their bonds and linkages and volatile matter is released as gas and a liquid product which evaporates off leaving a material with high carbon content . The high composition of the fixed carbon refers to high quality of the adsorbent which improves the surface area and adsorption performance. From the result the low ash content in the activated carbon indicates inorganic matter in the sample is insignificant. According to different scholar findings high fixed carbon, low moisture, low volatile matter and low ash content adsorbents are recommendable for adsorption activities (Fito et al. 2019;Mopoung et al. 2015;Pathania et al. 2017). Therefore the prepared activated carbon is efficient as it shown by various proximate analysis.
The specific surface area of the prepared activated carbon based on sear method analysis is presented in Table 2. Based up on this result the prepared adsorbent has very high surface area, it may arise from sodium hydroxide activation. Upon high concentration sodium hydroxide activation, leads to reorganization of the chemical constituents and subsequent deposition of carbon-rich molecules to the voids of biomass by the influence of temperature and pressure increase surface area of the adsorbent (Deng et al. 2011;Islam et al. 2015). This results agreed with the reported value of BET analysis of activated carbon in other scholar findings (Li et al. 2013).
Determination of pH pzc The point of zero charge is defined as the condition in which the density of electric charge on the adsorbent surface is zero. In this study, the solid addition method was followed. Accordingly, 0.01 M (50 mL) of NaCl solution poured into 12 flasks each containing 0.1 g of adsorbent. The pH of the solutions was measured from 2 to 12 by using a pH meter and kept for 24 h. The results were then plotted between "pH final versus pH initial". The point of intersection of the curves of "pH final versus pH initial, " is the PZC of adsorbent. The plot of pH final versus pH initial for both adsorbents is presented in Fig. 2. It was found to be 7.6. When the pH of the solution is below the PZC, the surface of the adsorbent will become positively charged and when the solution pH is greater than PZC, the surface of the adsorbent will become negatively charged (Temesgen et al. 2018). It implied that the prepared adsorbent was most probably adsorbing malachite green dye on basic regions.

Optimization results of different parameters Effects of solution pH
In fact that the solution pH can affect the surface charge of the adsorbent, the degree of ionization of the different pollutants, the dissociation of functional groups on the active sites of the adsorbent as well as the structure of the dye molecule (Ai et al. 2011;Bello et al. 2017;Ghaedi et al. 2014;Mall et al. 2005). Therefore the solution pH is a master parameter during the dye adsorption process. The effect of initial pH on the MG removal was studied in the pH range of 2-12 with initial dye concentration of 10 mg/L (50 mL) and adsorbent dose of 0.5 g and presented in Fig. 4. Removal efficiency increase with increasing solution pH until equilibrium reached. This is the fact that increasing pH leads to the formation of negative charge on the surface of adsorbent up on deprotonation reaction. This negative charge enables high removal efficiency as result of electrostatic attraction between the adsorbent and positively charged of adsorbate (MG). Whereas at lower pH, the various functional groups and reactive atom of dyes and adsorbent protonated and both get positive charge (Ai et al. 2011;Mall et al. 2005). Therefore, due to strong repulsive force between dyes and adsorbent decrease the removal percentage. As shown in Fig. 4 at acidic region (pH = 2) the removal efficient is 77.5% whereas at the basic region (pH = 10) is 98.8%. The removal efficiency is increase until the pH reaches to optimum beyond that slightly decrease due to competency of active site of the adsorbent.

Effects of adsorbent dose
To know the effects of the adsorbent dosage on MG removal efficiency the experiments was carried out by varying adsorbent dose from 0.2 to 1.4 g at fixed dye concentration (10 mg/L), pH = 10, contact time 60 min, shaking speed 400 rpm and presented in Fig. 5. When the bio mass increased from 0.1 to 0.5 g an increase in the MG removal from 87.7 to 98.8% percentage removal was observed. This behavior could be explained considering that with adsorbent dosage increases leads to an increase on the surface; consequently, more active sites are available to bind dye from aqueous phase (Ai et al. 2011;Li et al. 2013). At masses over 0.5 g, the amount of MG slightly decreased due to the aggregation and overlapping of particles of adsorbent in the solution, consequently, a decrease in the surface for dye uptake occurs. This result is in agreement with data reported by different scholar findings (Ai et al. 2011;Lee et al. 2019). For this reason, the adsorbent mass 0.5 g was chosen for the subsequent experiments.

Effects of initial concentration of dye
The effect of the initial concentration of MG dye on its adsorption onto the prepared adsorbent is presented in Fig. 6. The experiment was carried out at different concentration (50 mL of 10-50 mg/L) at fixed adsorbent dose 0.5 g, pH = 10, contact time 60 min, shaking speed 400 rpm at and room temperature in batch operation mode. As shown in Fig. 6 the percentage removal of MG decrease with increasing initial concentration of dye. Since the adsorbent dose is fixed, there is a fixed number of active site as a result percentage removal decrease with increasing concentration. At low initial concentrations of MG dye relatively high percentage sorption's were observed. As a result of the high ratio of adsorbent surface binding sites to the dye concentration, meaning that a fewer number of dye molecules were competing for the available binding sites on the adsorbent Dos Reis et al. 2011;Raval et al. 2016). Although, adsorption capacity (q e ) increases with increasing initial concentration of MG dyes. As increase the initial concentration of the dye from 10 to 50 mg/L, resulted an increase in adsorption capacity (q e ) from 0.988 to 4.55 mg/g. The increase in the initial concentration of the dye enhances the interaction between the dye molecules and the surface of the adsorbent (Ai et al. 2011;Lee et al. 2019;Mondal and Kar 2018). This results can also observed with different scholars finding and reported in different literatures (Mondal and Kar 2018;Raval et al. 2016).

Effect of contact time
The effect of contact time on the MG dye adsorption by the prepared adsorbent was carried out with different contact time (10-80 min) at fixed dose 0.5 g, pH = 10, shaker speed 400 rpm and presented in Fig. 7 below. The amount adsorbed dyes first rapidly increased, and then gradually decreased until equilibrium was reached. This is perhaps due to the initial availability of maximum number of active sites which gets saturated with time. As a result, the remaining vacant surface sites are difficult to be occupied due to the formation of repulsive force between the adsorbate (MG) on the solid surface of adsorbent with adsorbate (MG) on the bulk phase (solutions) as well as the saturation of active site of the adsorbent. This trend was observed by different scholar's findings and reported in different literatures (Mondal and Kar 2018;Rahmat et al. 2016). The removal efficiency was found to be at the range of 64.1 to 98.8% when the time rises from 10 to 60 min respectively. As shown in Fig. 7, the contact time required for MG to reach equilibrium was 60 min, with the removal efficiencies of 98.8%. The result showed that the prepared adsorbent has short equilibrium time which shows the adsorbent have enough number of active site for a given concentration. In fact short equilibrium time is recommendable on the view of water treatment technologies.

Kinetics studies
The kinetic profile is fundamental to study an adsorption system. Kinetic curves provides information about the adsorption rate and also, regarding to the required time to attain the equilibrium (Dos Reis et al. 2011;Ghaedi et al. 2014;Royer et al. 2009). In the present studies, adsorption kinetics was studied using the pseudo-first order (Eq. 9), pseudo second order (Eq. 10) and antiparticle diffusion model (Eq. 11) respectively (Rahmat et al. 2016;Regti et al. 2017).
where q e (mg/g) is amount adsorbed at equilibrium time; q t (mg/g) is amount adsorbed at time, t (min); k 1 is the pseudo-first-order rate constant; k 2 is the pseudo secondorder rate constant; k diff (mg/g min 1/2 ) is the intraparticle diffusion rate constant; and C is the intercept that indicates the boundary layer thickness. The kinetic rate constant, k, and q e for each model can be calculated by plotting graph log (q e − q t ) versus t for pseudo-first-order, t/q t versus t for pseudo-second-order models, and q t versus t 1/2 for intraparticle diffusion models and the graphs presented in Figs. 8, 9, and 10, respectively.
All the kinetic parameters for all kinetics models were calculated from the graph and presented in Table 3. As shown in Table 3, amount of adsorbed dyes (q e ) or q e calculated based on pseudo-second order models very similar to experimental value as compare to pseudo 1st order and inter particle diffusion mode. Furthermore, the correlation factor (R 2 ) obtained calculated through pseudosecond-order models (R 2 = 0.99684) greater than pseudo 1st order and inter particle diffusion model. This implies that the experimental data were good agreement with pseudo second kinetics order model (Rahmat et al. 2016).

Equilibrium isotherm studies
Adsorption isotherms describe how the adsorbate interacts with adsorbent and provide comprehensive understanding about the nature of the interaction. Isotherms help to provide information about the optimum use of adsorbents (Raval et al. 2016). Isotherm curves are extremely relevant for adsorption purposes, since it provides information about the interaction mechanisms and maximum adsorption capacity of a determined adsorbent (Leechart et al. 2009;Regti et al. 2017). In order to determine the best-fit bio-sorption isotherm model, the equilibrium data were analyzed by most common isotherm models such as the Langmuir and Freundlich isotherm models. They were helpful to determine the maximum adsorption capacity of adsorbate for the given adsorbent. They differ in the basic assumptions, shape of the isotherm and nature of the adsorbent surface. The Freundlich isotherm is derived by assuming a heterogeneous surface with a non-uniform distribution of heat of adsorption over the surface. Whereas in the Langmuir theory, the basic assumption is that the sorption takes place at specific homogeneous sites within the adsorbent Deng et al. 2011). The mathematical expressions for those isotherms were presented in equation (13) log q e = log k f + log C e n ; where C e is the equilibrium concentration of solute (mmol/L), q e is the amount of solute adsorbed per unit weight of adsorbent (mmol/g of adsorbate), q m is the adsorption capacity (mmol/g), or monolayer capacity, and b is a constant (L/mmol) for Langmuir isotherm, K f and n are empirical constants for Freundlich isotherm incorporating all parameters affecting the adsorption process such as, sorption capacity and sorption intensity respectively. The isotherm curves were drawn C e / q e versus C e for Langmuir isotherm and logq e vs. logc e graph for Freundlich isotherm model and presented in Figs. 11, 12 respectively. The isotherm parameters such as, q m and b for Langmuir isotherm model can be calculated from intercept and the slope of C e /q e versus C e graph respectively. The value of k f and n for Freundlich can be calculated from logq e vs. logc e graph. All the isotherm parameters calculated from the graph and correlation factor (R 2 ) for both models were presented in Table 4 below. As shown in Table 4 the collation factor for Freundlich (R 2 = 0.98596) close to 1 confirms Freundlich isotherm model better describes the interaction between adsorbent and adsorbate in aqueous system.   The Adsorption was considered as satisfactory when the Freundlich constant n took value within the range 1-10. Therefore the value of n calculated from the graph is lies on this range and Freundlich considered as satisfactory to describe adsorption. For Langmuir type adsorption process, the efficiency of the adsorption process could be predicted by the dimensionless equilibrium parameter R L , which is defined by the following equation in Eq. 14 (Ajenifuja et al. 2017;Li et al. 2013). (14) where b is Langmuir constant related to the energy of adsorption (L/mg) and C 0 is initial concentration (mg/L). The calculated R L values at different initial dye concentration were written in Table 5 below. R L value indicates the adsorption nature to be either unfavorable if R L > 1), linear if R L = 1, favorable if 0 < R L < 1 and irreversible if R L = 0 (Ajenifuja et al. 2017). For this study all the valves were lies between 0 and 1 which confirming that the adsorption of dye over the adsorbent was favorable (Ajenifuja et al. 2017).

Proposed adsorption mechanism
The adsorption of MG dye from aqueous solution by activated carbon derived from Catha edulis stem is strongly dependent on the various functional groups on the surface of Catha edulis stem such as hydroxyl, phenols, aromatics and etc. which are supported by FTIR spectral results described in Fig. 3. The surface of Catha edulis functional groups may be charged (negative and positive) or neutral upon protonation and deprotonation. The possible adsorption mechanism of MG dye on the surface of Catha edulis is summarized in Fig. 13 and the probable adsorption mechanisms between the surface functional groups of Catha edulis adsorbent and MG dye can be assigned to the various interactions such as electrostatic attractions, hydrogen bonding interaction and π-π interactions between the adsorbent and adsorbate (Jawad et al. 2019). Similar observation was reported for the adsorption on MG on chemically modified rice husk (Chowdhury et al. 2011). The comparison of previous study on the adsorption of MG dye by different adsorbents with the current finding is presented in Table 6.

Conclusions
The present investigation showed that activated carbon prepared from khat (Catha edulis) stem is an effective adsorbent for removal MG from aqueous solution. The effect of different parameters like pH, contact time, adsorbent dose and initial concentration of dye were tested. Removal of MG is pH dependent and the maximum removal was attained at basic medium pH = 10 with 98.8% percentage removal. The bio sorption MG dye at the basic medium indicated that surface charge greatly affected the dye uptake capacity. Adsorption equilibrium data tested on Langmuir and Freundlich models and equilibrium data fitted very well in Freundlich isotherm equations. The maximum MG sorption