RESEARCH ARTICLE

 

Liquid Phase Adsorption of Rhodamine B Dye onto Acid-treated Raphia hookeri Fruit Epicarp: Isotherms, Kinetics and Thermodynamics Studies

 

 

Adejumoke Abosede Inyinbor^{I, *}; Folahan Amoo Adekola^II; Gabriel Ademola Olatunji^II

^IDepartment of Physical Sciences, Landmark University, P.M.B 1001, Omu Aran, Nigeria
^IIDepartment of Industrial Chemistry, University of Ilorin, P.M.B 1515, Ilorin, Nigeria

 

 

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ABSTRACT

Novel adsorbent was prepared from the waste of Raphia hookeri fruit via acid treatments (ARH). The Brunauer-Emmett-Teller (BET) surface area of ARH was obtained to be 1.86 m² g^-1. Large surface pores evidently exposed by the scanning electron microscopic studies characterized ARH. Active surface functional groups were also revealed by the infrared spectroscopic studies. These characteristics resulted in ARH effectiveness in Rhodamine B (RhB) dye removal, with 98.46 % dye removal from 50 mg L^-1 RhB solution. Maximum adsorption was obtained at pH of 3. Equilibrium adsorption data fitted best into the Langmuir adsorption isotherm, with maximum monolayer adsorption capacity of 166.67 mg g^-1. Pseudo-second-order kinetics best describe the RhB-ARH adsorption kinetic data. Energy of adsorption obtained from the D-R model was greater than 8 kJ mol^-1, suggesting that the uptake of RhB onto ARH was chemical in nature. Desorption efficiency followed the order CH₃COOH > HCl > H₂O with highest desorption percentage of 36.36 %.

Keywords: Raphia hookeri, biomass, rhodamine B, kinetics.

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1. Introduction

Water pollution has become a global challenge. The desire for wealth creation continues to spur up various industries; thereby resulting into release of various toxicants into the environment.¹ Discharges from dye-consuming industries contain loads of dye molecules identified at first by their colours. Dye molecules persist in the environment, their colours impede light penetrations into the water body, and reduces dissolved oxygen, thus threatens aquatic ecosystems and organism; as well as poses serious health challenges to human.² For instance, RhB, a xanthenes dye widely used in various dye-utilizing industries is known to cause respiratory, eye and skin irritations, as well as gastrointestinal disorders.³ Effective treatment of effluents laden with RhB or other dyes, should be implemented before their discharge into the environment.

Industries within the developing economy avoid conventional methods of effluents treatments due to their economic implications, limitations, and complexities. The easy operational techniques as well as ability to remove very low concentrations of pollutants gave adsorption using activated carbon an advantage over other conventional methods of effluents treatment.⁴ The use of activated carbons in effluent treatment dates back to an-cientlndian and Egyptian days. Raphael von Ostrejko, however, developed and patented the commercial activated carbon currently in use during the late 19th/early 20th century.⁵ Activated carbon has been greatly used in the treatment of effluents with loads of organic compounds.⁶ However, since the high cost of activated carbon is as a result of the precursors in use for their preparation, environmentalists therefore seek other precursors as well as alternative sorbent.^7,8 Various low-cost bioadsorbents such as clay, industrial wastes, and agricultural wastes have textural, structural, and compositional potentials to serve as alternatives to activated carbon.

Agricultural wastes, as well as other waste materials such as coconut husk,⁷ rice husk,⁹ tamarind wood,¹⁰ Peach stone,¹¹ cocoa pod husk,¹² Bamboo,¹³ Periwinkle shell,¹⁴ sugar cane bagasse,¹⁵ Apricot stone,¹⁶ peanut shell,¹⁷ corncob,¹⁸ apple wastes,¹⁹ wood saw dust,²⁰ Bengal gram husk,²¹ Moroccan clay,²² Peat and coconut fibres,²³ Lentibulariaceae,²⁴ waste pea shell,²⁵ chir pine saw dust,²⁶ as well as Raphia hookeri fruit epicarp,^27;have been utilized as cheap alternatives for activated carbon preparations and biosorbents for various pollutants uptake.

Several advantages accompany the use of biosorbents in the treatment of wastewater. They include environmental protection and waste management. Materials that would have ordinarily been disposed off, have become useful environmental remediation tools. Another advantage is the availability of abundant and inexhaustible/renewable material sources. Most importantly, the surface of a biosorbent can be tailored towards the uptake of a specific pollutant or a group of pollutants, via surface modification or functionalization. Surface modification and/or functionali-zation, affects the surface chemistry of a biosorbent and may also improve adsorption potential. Acid treatment for instance, is known to increase adsorbent porosity vis-á-vis its surface area.²⁸ Consequently, increase in the porosity of adsorbent will increase its adsorption potential.

In our previous work,²⁹ we employed a new approach of biomaterial fibre impregnation using concentrated acid and subsequent thermal treatment in order to blow the fibre open, thus leaving large pores on the biomaterial surface. Such large pores could act as medium for transporting large molecules into the adsorbent. Dika nut waste was utilized as biomaterials. This work, however, utilized a novel biomass (Raphia hookeri fruit epicarp), which belongs to the Palmaceae family. Waste from this family is usually characterized by high fixed carbon content, thus making them good precursor for activated carbon preparation. To the best of our knowledge, the application of this biomass in environmental remediation has not been earlier reported. We recently reported the use of raw RH in RhB uptake.²⁷ However, in a bid to enhance sorption capacity, in this study, RH was modified via acid treatment. Considering the wide usage of RhB, its toxicity as well as the great desires for a clean and sustainable environment, such studies as this is of great importance. The present study therefore reports the uptake of Rhodamine B (RhB) dye from aqueous solution, onto the prepared novel adsorbent, with focus on various adsorption operational parameters. Detailed kinetics, isothermal, as well as thermodynamics studies of the adsorption system; are reported. Adsorption mechanism and desorption studies were employed to justify the mode of RhB uptake onto the prepared adsorbent. Statistical tools were also employed to establish the best kinetic, as well as isotherm model for the adsorption studies.

 

2. Materials and Methods

2.1. Materials

Analytical grade reagents were used, hence no purification was carried out on them. Sigma Aldrich supplied concentrated H₂SO₄ while BDH supplied RhB. The chemical structure of Rhodamine B is presented in Fig. 1, while the characteristics of RhB are listed in Table 1. Raphia hookeri (RH) epicarp were collected from local farmers in Makogi, Edu local government, Kwara State. Nigeria.

 

 

 

 

2.2. Adsorbate Preparation

A 1000 mg L^-1 stock solution of RhB was prepared by dissolving accurately weighed mass of RhB in 1 dm³ deionized water. Other working solutions that are of lower concentrations were subsequently prepared from the parent solution.

2.3. Biomass Pretreatment and Adsorbent Preparation

RH was thoroughly washed and dried in an oven, operated at low temperature over night. Subsequently washed, dried biomass was pulverized and screened into a particle size of 150-250 µm. Raphia hookeri (RH) fruit epicarp was treated using concentrated sulphuric acid as described in our earlier reported work.²⁹ ARH was subsequently stored in airtight containers for further characterization and applications.

2.4. Adsorbent Characterization

The characteristics of adsorbent surface is quite important in adsorption studies, hence the surface chemistry, surface area and surface morphology, were investigated.

2.4.1. Surface Chemistry Determination

A Bruker Alpha FTIR spectrometer was used for functional group analysis. Discs preparation was done using an agate morta. The adsorbent (ARH) and KBr (Merck, for spectroscopy) were mixed in a ratio 1 to 500, and the mixture was subsequently pressed at 10 tonnes cm^-2 for 15 min under vacuum. The pH point of zero charge determination (pHpzc) gives insight into the adsorbent surface charge in different solution media. This was done by transferring 50 cm³ NaCl solution into series of nine conical flasks. The pH of the solutions was adjusted with NaOH or HCl between pH 2 and 10. A 0.1 g of the adsorbent was added to each of the flask; and the containers were sealed and placed on a shaker for 24 h after which the final pH was measured. The difference between the initial and final pH were calculated and plotted against the pH initial. The point of intersection of the resulting curve with vertical axis gave the pHpzc.

2.4.2. Surface Area and Porosity Analysis

BET surface area and average pore diameter were determined using a Micrometrics Tristar II surface area and porosity analyzer. Samples were degassed under vacuum at 90 °C for 1 h and the temperature was further ramped up to 200 °C overnight.

2.4.3. Surface Morphology and Elemental Composition

The surface morphology and elemental analysis were done using FEIESEM Quanta 200 for SEM and EDX.

2.5. Batch Adsorption Studies

2.5.1. Effects of Adsorbate pH

A0.1 g of ARH was added to 100 cm³ of 100 mg L^-1 RhB solution whose initial pH had been varied between 2 and 10 using 0.1 M HCl or 0.1 M NaOH. The mixture was agitated for 4 h on a thermostated water bath shaker, operated at a temperature of 26 °C and speed of 130 rpm. The supernatant was separated using a centrifuge and the concentration of unadsorbed dye was determined using a Beckman Coulter Du 730UV-visible spectrophotometer operated at 554 nm. Percentage removal was calculated according to Equation 1. The optimum pH obtained was used in subsequent adsorption studies.

where Ci and Cf are concentrations of RhB in solution at initial and at a given time t, respectively.

2.5.2. Effects of Initial Adsorbate Concentration/Contact Time Varying RhB concentration (50 mg L^-1 to 400 mg L^-1) was utilized for this study. 0.1 g of ARH was agitated with 100 cm³ of RhB solution of each concentration in different 250 cm³ flasks. Samples were withdrawn at different time intervals, centrifuged and the supernatant was analyzed for change in dye concentration using a UV-visible spectrophotometer. This process continued until equilibrium was attained. The quantity of RhB adsorbed at a given time q_t, (mg g^-1) was calculated using:

where C_iand C_tare concentrations of RhB in solution at initial and at time t, V is the volume in litre and M is the mass of the adsorbent in g.

2.5.3. Effects of Adsorbent Dosage

A given dose of the adsorbent (betweenlgL^-1 and5gL^-1) was agitated with 100 cm³ solution of RhB at a given time. Other conditions such as agitation speed, temperature, and initial concentration were maintained at 130 rpm, 26 °C and 100 mg L^-1, respectively. Unadsorbed dye was determined as earlier described and percentage dye removal was calculated.

2.5.4. Effects of Temperature

Adsorptions of RhB onto the prepared adsorbents were investigated as a function of temperature, 100 cm³ initial dye concentration of 100 mg L^-1 was added to1gL^-1 of each adsorbent in separate 250 cm³ glass conical flask. The mixture was then agitated at 130 rpm for a predetermined time while varying the temperature between 303 and 333 K. Unadsorbed dye was determined as earlier described and percentage dye removal was calculated.

2.6. Mathematical Modelling

Isotherms and kinetics models give insight into adsorption types and mechanism. Four isotherms and five kinetics models was employed to analyze the adsorption data in this study. Feasibility and spontaneity of the adsorption process was ascertained via thermodynamic studies.

2.6.1. Isotherms Models

Langmuir isotherm³⁰ assumes that adsorbate molecules bind to a uniform surface. Langmuir equation is expressed in Equation 3. C_eand q_eare concentration of adsorbate in solution at equilibrium measured in mg L^-1 and quantity of dye adsorbed at equilibrium in mg g^-1, respectively. q_maxis the maximum monolayer adsorption capacity of adsorbent (mg g^-1) and K_Lis the Langmuir adsorption constant (L mg^-1). The dimensionless R_Lwhich explains the favourability of the adsorption process can be obtained from Equation 3a.

Freundlich isotherm³¹ describes a multilayer adsorption. Mathematical Equation 4 expresses this isotherm model. C_e and q_eare concentration of adsorbate in solution at equilibrium measured inmgL^-1 and quantityofdye adsorbed atequilibrium in mg g^-1, respectively. K_fand n are Freundlich constants incorporating the factors affecting the adsorption capacity and adsorption intensity, respectively.

Temkin isotherm,³² which assumes linear rather than logarithmic decrease of heat of adsorption while ignoring extremely low and very high concentration. Temkin equation is expressed by Equation 5. A (L g^-1) and B are Temkin isotherm constants, b (J mol^-1) is a constant related to the heat of absorption and can be determined using Equation 5a. Where T is the absolute temperature (K) and R is the gas constant (J mol^-1 K).

Dubinin Radushkevich (D-R) model³³ gives insight into the biomass porosity as well as the adsorption energy. D-R model is expressed by Equation 6, Polanyi potential (є) and the mean energy of adsorption (E) can be obtained by Equations 6a and 6b, respectively. The value of adsorption energy (E) obtained from the D-R model further provides information as to whether adsorption process is physical or chemical in nature, β which is the activity coefficient helps in obtaining the mean sorption energy E (kJ mol^-1).

2.6.2. Kinetics Model

In order to understand the adsorption process better, the pseudo-first-order kinetics model of Lagergren,³⁴ pseudo-second-order,³⁵ Elovich,³⁶ and Avrami,³⁷ kinetics models were used to test the kinetics data while the intraparticle diffusion ofWeber and Morris³⁸ investigated the mechanism of adsorption.

The pseudo-first-order kinetics model is expressed mathematically by Equation 7, q_eand q_tare quantity of RhB adsorbed at equilibrium, and at time t (mg g^-1), respectively, k₁is the pseudo-first-order rate constant (min^-1);

Pseudo-second-order kinetic model expressed by Equation 8, q_e and q₁are quantity of RhB adsorbed at equilibrium, and at time t (mg g^-1), respectively, while k₂ is the pseudo-first-order rate constant (g mg^-1 min^-1);

Elovich kinetic model is expressed by Equation 9, the Elovich constants a and β may explain the chemisorption rate and extent of surface coverage, respectively.

Avrami kinetic model is expressed by Equation 10, K_AV and n_AV whichcan be obtained fromthe interceptand slope ofthe plotof ln[-ln(1 - a)] against lnt are the Avrami constant and the Avrami model exponent of time related to the change in mechanism of adsorption.

The intraparticle diffusion model by Weber and Morris is expressed by Equation 11, adsorption mechanism is well explained by the plot of quantity adsorbed at time t (q_t) against the square root of time (t). A single linear adsorption profile or a multilayer adsorption profile may result from the plot of q_t against t^1/2and C is the boundary layer thickness.

2.6.3. Validation of Adsorption Kinetics

Kinetics and isothermal models were validated using Sum square of error (SSE), chi-square (x²) and the normalized standard deviation (∆q_e%), represented by Equations 12, 13 and 14;

 

2.6.4. Thermodynamic Studies

Thermodynamic parameters that explain feasibility, spontaneity and the nature of adsorbate-adsorbent interactions (AG°, AH° and AS°) were calculated using the mathematical relations 15 and 16;

where T is the temperature in Kelvin, R is the gas constant and Ko can be obtained from equilibrium concentration and quantity adsorbed at equilibrium. The values of enthalpy (∆H°) and AS° can be obtained from the plot of lnKo versus 1/T.

2.7. Spent Adsorbent Regeneration Studies

Adsorbents regeneration is very important in adsorption study, thus leaching/desorption of RhB from adsorbent surface was investigated using three eluents (water, 0.1 M HCl and 0.1 M CH₃COOH). A fixed mass of fresh adsorbent was loaded with RhB by agitation it with a fixed volume and a fixed concentration of RhB at its optimum pH for 120 min. The loaded adsorbent was separated by centrifugation and the residual RhB concentration determined spectrophotometrically. RhB loaded adsorbent was subsequently washed with water gently to remove unadsorbed dye. Dry loaded adsorbent was contacted with 100 cm³ of each desorbing eluent and was shaken for a predetermined time. The desorbed RhB was determined spectrophotometrically and the desorption efficiency was calculated using the mathematical relation 17;

Where q_de is the quantity desorbed by each of the eluent and q_ad is the adsorbed quantity during loading.

 

3. Results and Discussion

3.1. Characteristics of ARH

Low ash content characterized ARH (Table 2), this suggests that ARH is easily degradable. The pH and the pHpzc are near neutral suggesting that percentage RhB adsorption is expected to increase as adsorbate solution pH increases. The BET surface area of ARH is low (1.86 m² g^-1), low surface area is a characteristic of agro waste.³⁹ Agro waste framework is lined with various functional groups thus resulting into low porosity.^40,41 Low affinity for water, high carbon content and bulk density all presents ARH a suitable adsorbent for dye uptake.³⁹

 

 

Figure 2a, b shows the FTIR spectral of RH and ARH before RhB uptake and FTIR spectrum of ARH after RhB uptake, respectively. Vivid absorption bands occurs at 1108 cm^-1, 1293 cm^-1, 1384 cm^-1, 1595 cm^-1 and 3288 cm^-1, this corresponds to C-OH or C-N stretching vibrations, C-O-C vibrations of lignin, C-C vibrations of aromatics, C=C vibrations of aromatic and O-H or N-H stretching vibrations, respectively. In RH observed peak at 2843 cm^-1 corresponds to -C-H vibration of methylene. Elimination of volatile compounds and breakdown of hemi-cellulose resulted into the disappearance of methylene vibration band after acid treatment. After RhB adsorption, shift in various absorption bands occurred suggesting that there corresponding functional group may have participated in RhB uptake.⁴² A new peak was also observed at 1716 cm^-1, this corresponding to C=O stretching vibrations of carboxylic group in RhB.

 

 

SEM micrograph of ARH before and after RhB adsorption is shown in Fig. 3a,b. ARH surface was observed to be smooth and with pores of various shapes and sizes; these pores may serve as medium for RhB absorption. The surface of ARH was, however, left rough after RhB uptake (Fig. 3b).

3.2. Batch Adsorption Studies

3.2.1. Effects of pH on RhB Uptake onto ARH

The effects of initial solution pH on RhB uptake is depicted in Fig. 4. Optimum adsorption (86.79 %) was observed at pH of 3. RhB existence varies depending on the solution media, RhB may exist in its cationic form in solution pH range of 1 to 3, lactonic form in solution pH of less than 1 and its zwitterionic form in solution with pH greater than 3.7. Adsorbent surface charge is also very important in pH study. The pHpzc of ARH obtained was 6.8 (Table 2). At pH below the pHpzc, the surface of the adsorbent is positively charged thus electrostatic repulsion between cationic RhB and adsorbent surface may result into low adsorption. As the pH of the solution increases, however, more sites are created for RhB adsorption thus RhB uptake increases. This phenomenon was obeyed between pH of 2 and 3. Zwitteri-onic form of RhB, however, facilitates its dimer formation due to the attraction between the xanthenes and the carboxyl groups of the monomers. At above pH of 3.7 therefore large molecules of RhB are formed (dimer) thus adsorption becomes difficult. Maximum adsorption at pH of 3 have been previously reported by researchers.^43,44,45

 

 

 

3.2.2. Effects of Adsorbent Dosage on RhB Uptake onto ARH Rapid increase was observed in percentage adsorption when

the adsorbent dosage was increased from 1 gL^-1to2gL^-1 (Fig. 5). Increase in available adsorption site may have been responsible for this rapid increase. However, as the adsorbent dosage further increased, negligible increase was observed in percentage adsorption and percentage adsorption subsequently goes to equilibrium at dosage of4gL^-1. Saturation of adsorption sites results into no further adsorption at high adsorbent dosage.⁴⁶

 

 

3.2.3. Effects of Concentration/Contact Time on RhB Uptake onto ARH

For all the initial adsorbate concentrations considered, adsorption of RhB onto ARH was observed to be first rapid, followed by a gradual adsorption and subsequently equilibrium was attained within 120 min. The initial rapid adsorption may have been to the surface of the adsorbent while the gradual adsorption results from continuous bombardment that aids percolation of RhB molecules into ARH pores. Various functional groups present on the surface of ARH may have been responsible for the surface adsorption. Surface modification was found to enhance adsorption capacity of ARH. Comparing ARH with RH in our recently reported work²⁷ about 12 % increase in quantity of RhB adsorbed was recorded. Quantity adsorbed at equilibrium ranged between 49.23 mg g^-1 and 360.12 mg g^-1. Quantity of RhB dye adsorbed at high concentration was observed to be higher when compared with our previously reported work.²⁹ The low value of Aq_efor the Temkin isothermal studies suggests that adsorbate-adsorbate interactions may have occurred in the RhB-ARH system, this may account for high quantity adsorption recorded at high concentration. High initial concentration also provides enough driving force to overcome the mass transfer barrier between the aqueous and solid phase thus high adsorption at high concentrations.

3.2.4. Effects of temperature on RhB uptake onto ARH

Quantity adsorbed decreased with increase in temperature, only about 23 mg g^-1 RhB was adsorbed at 60 °C (Fig. 7). The dye molecule may have more affinity for H₂O than adsorbent surface at high temperature. Break of established bonds between the RhB dye and adsorbent may also occur at high temperature thus resultingin decrease in quantity adsorbed at high temperature.⁴⁷

 

 

 

 

3.3. Adsorption Isothermal Studies

Isotherm parameters for the adsorption of RhB onto ARH are listed on Table 3. The dimensionless separation factor (R_L) value obtained was 0.002, suggesting that adsorption process was favourable. The Freundlich isotherm constant n with a value greater than unity also corroborates favourable adsorption within the RhB-ARH system. The initial rapid adsorption that characterized the uptake of RhB onto ARH (Fig. 6) may have been onto a uniform site as a result of contact with activated surface functional groups. This is justified by the high R²value of the Langmuir isotherm model as well as low x²and ∆q_evalues (Table 3). Although monolayer adsorption dominates the uptake of RhB onto ARH, however, the R²value for the Freundlich adsorption isotherm obtained was 0.9060. Thus adsorption onto other surfaces such as percolation of RhB into the pores of ARH may also have occurred. The energy of adsorption as calculated from the D-R isotherm model is greater than 8 kJmol^-1 (Table 3) suggesting that the uptake of RhB onto ARH follows a chemical method. The maximum monolayer adsorption capacity (q_max) obtained to be 166.67 mg g^-1 was compared with others previously reported in the literatures (Table 4) and ARH can be said to have exhibited better performance.

 

 

 

 

3.4. Adsorption Kinetics Studies

Adsorption kinetics have a great effect on adsorbent efficiency, it describes the rate of pollutant (adsorbate) uptake onto the adsorbent as well as controls the equilibrium time. Insight into adsorption mechanism was further established using the pseudo-first, pseudo-second, Elovich and Avrami kinetics models. Close agreement exists between the q_caland q_expfor the pseudo-second-order kinetics model (Table 5), low SSE, Aq_e and ² as well as high R²values recorded for the pseudo-second-order kinetics model suggests a good fitting of the kinetic data into this model. The adsorption data fitted well into the pseudo-second-order kinetic models thus indicating that uptake of RhB onto ARH may be chemical in nature.⁵⁵ Pseudo-first-order and Avrami kinetics models are not suitable for the RhB-ARH adsorption system. Elovich model is known to best describe a chemisorption adsorption mechanism system.⁵⁶ Although low values were recorded for SSE, Aq_eand ² for the Elovich model, the pseudo-second kinetics better describes the kinetics of RhB-ARH system. A two stage adsorption profile was obtained for ARH-RhB system for initial concentration of 100 mg L^-1 to 400 mg L^-1 while a single linear profile obtained for initial concentration of 50 mg L^-1 suggest a single stage adsorption process (figure not shown). For the multilinear profile, the first steeper portion can be attributed to the boundary layer diffusion of RhB while the second linear portion corresponds to a gradual sorption stage where intraparticle diffusion was the rate-limiting step and subsequently equilibrium was attained. Boundary layer diffusion may have dominated the uptake of RhB onto ARH in the 50 mg L^-1 solution due to the ratio of available surface adsorption site and the RhB concentration in solution.

3.5. Adsorption Thermodynamics

Table 6 lists the calculated thermodynamic parameters and for the Van't Hoff plot. Negative enthalpy (∆H°) was obtained for the uptake of RhB onto ARH, this suggests that the adsorption process was exothermic in nature while the negative values of AS° (Table 6) indicate decrease in the randomness at the solid-liquid interface during the adsorption of RhB onto ARH.

 

 

∆G° values obtained for temperature range between 303 and 323 °K were negative, negativity of AG° decreased as the temperature increased and for the highest temperature considered (333 °K), AG° was found to be positive. This suggests that the spontaneity of the adsorption process decreased as temperature increased. The adsorption process was, however, more favourable at lower temperature. Chen el al. 2012,⁵⁷ previously reported similar trend when they utilized Resin D301 in glyphosate adsorption.

3.6. Desorption Studies of RhB-ARH System

The desorption efficiencies by the three eluents used was found to be generally low with neutral H₂O having the lowest desorption efficiency (4.55 %). Percentage desorption for HCl and acetic acid were recorded to be 31.82 % and 36.36 %, respectively. Desorption efficiency followed the order CH₃COOH > HCl > H₂O. Chemisorption dominates the mechanism of RhB uptake onto ARH, this is well justified by the percentage desorption efficiency recorded using CH₃COOH. Possibility of low desorption is high for adsorbents with so many adsorption sites. Various surface functional groups in ARH facilitate several contacts points between the dye molecule and ARH thus large net adsorption energy and subsequently difficult dye desorption from adsorbent surface.⁵⁸

 

4. Conclusion

ARH, an adsorbent with multifunctional group surface was highly effective in the uptake of RhB from aqueous solution. Monolayer adsorption dominates the uptake of RhB onto ARH as the equilibrium adsorption data fitted best into the Langmuir adsorption isotherm. Some multilayer adsorption also occurred in the RhB-ARH system, with R²value of Freundlich adsorption isotherm being greater than 0.9. The maximum monolayer adsorption capacity obtained was 166.67 mg g^-1, and was found to be more effective than other adsorption systems previously reported in the literatures. The pseudo-second-order kinetics, energy of adsorption obtained from the D-R model as well as desorption efficiency suggests that uptake of RhB onto ARH was chemical in nature.

 

Acknowledgement

The authors gratefully acknowledge Miss Fola Oyinloye for linguistic editing of this work

 

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Received 30 May 2016
Revised 9 August 2016
Accepted 12 August 2016

 

 

* To whom correspondence should be addressed. E-mail: ¡nylnbor.adejumoke@landmarkunlverslty.edu.ng