Research Article  Open Access
M. Srinivas Kini, M. B. Saidutta, V. Ramachandra Murty, "Studies on Biosorption of Methylene Blue from Aqueous Solutions by Powdered Palm Tree Flower (Borassus flabellifer)", International Journal of Chemical Engineering, vol. 2014, Article ID 306519, 13 pages, 2014. https://doi.org/10.1155/2014/306519
Studies on Biosorption of Methylene Blue from Aqueous Solutions by Powdered Palm Tree Flower (Borassus flabellifer)
Abstract
Biosorption experiments were carried out for the removal of methylene blue (MB) using palm tree male flower (PTMF) as the biosorbent at various pH, temperature, biosorbent, and adsorbate concentration. The optimum pH was found to be 6.0. The kinetic data were fitted in pseudofirstorder and secondorder models. The equilibrium data were wellfitted in Langmuir isotherm and the maximum equilibrium capacities of the biosorbent were found to be 143.6, 153,9, 157.3 mg/g at 303, 313, and 323 K, respectively. Thermodynamic data for the adsorption system indicated spontaneous and endothermic process. The enthalpy and entropy values for adsorption were obtained as 15.06 KJ/mol and 0.129 KJ/mol K, respectively, in the temperature range of 303–323 K. A mathematical model for MB transported by molecular diffusion from the bulk of the solution to the surface of PTMF was derived and the values of liquid phase diffusivity and external mass transfer coefficient were estimated.
1. Introduction
Dyes are widely used in industries such as textiles, rubber, cosmetic, paper, carpet, printing, and leather and are wellknown pollutants of receiving bodies in the industrial areas. The release of dyes into waste waters by various industries causes serious environmental problems due to their toxicity and carcinogenicity and this poses a serious hazard to aquatic living organism [1]. However, waste water with dyes is very difficult to treat, since the dyes are recalcitrant organic molecules, are resistant to aerobic digestion, and are stable to light, heat, and oxidizing agents [2]. Methylene blue (MB) is not regarded as acutely toxic, but it can cause various harmful effects such as nausea, vomiting, diarrhea, gastritis, abdominal, chest pain, severe headache, profuse micturition, and methemoglobinemialike syndrome [3].
The most commonly used methods for color removal are biological and chemical precipitation. However, these processes are effective and economical only in cases where solute concentrations are relatively high [4]. In the case of relatively low concentration, adsorption is considered to be superior to other techniques due to its low cost, simplicity of design, high efficiency, and ease of operation [5]. Adsorption on activated carbon has been shown to be very effective for removal of dyes and other pollutants from aqueous solutions due to its large surface area, microporous structure, high adsorption capacity, and so forth. However, its commercial use is limited because of its high cost of manufacturing and problems associated with regeneration or disposal of spent carbon [6].
In recent times, there has been increased interest in the use of plant waste products for dye removal by adsorption from aqueous solution because of their natural availability and higher removal efficiency. Many researchers have studied the adsorption of methylene blue dye using plant waste such as peanut hull [7], castor seed shell [8], coconut shell [9], guava leaf [10], neem leaf [3], phoenix tree leaf powder [11], teak tree bark powder [12], and gulmohar plant [13]. Plant wastes are lignocellulosic materials that consist of three main structural components which are lignin, cellulose, and hemicelluloses [14].
In the present study, palm tree flower (male) was used as biosorbent for removal of MB. Palm tree male flower (PTMF) is an inexpensive and abundantly available material. Batch studies were carried out involving process parameters such as pH, biosorbent dosage, initial dye concentration, and temperature. The influence of these parameters on adsorption capacity was investigated. The adsorption data were fitted using suitable isotherm. A new mathematical model was derived and the values of liquid phase diffusivity and external mass transfer coefficient were estimated.
2. Mathematical Model
Since the particle is small, the flow in the vicinity of the particle is not turbulent. Thus we assume that the mass transfer to the particle can be modeled as a process of diffusion in a quiescent medium. Assuming pseudosteady state, the differential equation is Solving this equation with boundary condition, where is the concentration in bulk phase. The concentration profile in the liquid is obtained as The flux at the surface () is obtained as . This corresponds to a mass transfer coefficient (m/s): where is the liquid phase diffusivity (m^{2}/s).
Material balance for the solute is Further, rate of accumulation of solute on the solid is equal to the rate of mass transfer from the liquid; that is, Since equilibrium prevails on the surface, and are related by the Langmuir isotherm.
The Langmuir isotherm is given by Therefore in (6) can be substituted in terms of . Thus we obtain (8). Using (5) in (8), we obtain (9): where is solid loading (kg/m^{3} of liquid) and is concentration on the biosorbent surface (kg/m^{3}).
Solving (8) and (9) as an initial value problem using initial condition ; ; , , with a help of numerical computer program in MATLAB, yields the bulk concentration as a function of time. The liquid phase diffusion coefficient is obtained by matching the experimental concentration decay curve with that obtained from the model.
3. Materials and Methods
3.1. Adsorbate
Methylene blue (C.I. name: basic blue 9, class: Thiazine and C.I. number: 52015) is a cationic dye with a molecular formula C_{16}H_{18}N_{3}SCl and molecular weight of 319.9 g/mol and was purchased from Himedia, Bangalore. The MB (>99% dye content) was chosen because of its known strong adsorption onto solids. The maximum absorption wavelength of this dye is 665 nm. The structure of MB is shown in Figure 1.
3.2. Preparation of Biosorbent
Palm tree male flower (PTMF) collected from a farmhouse in Udupi, India was washed thoroughly with distilled water to remove surface adhered particles and water soluble materials. The PTMF was dried at 70°C for 2 days in a hot air oven and then cut into pieces, ground in a ball mill, and sieved to obtain average particles of 150 m. The PTMF powder was stored in an air tight container for further use. No other chemical treatments were used prior to adsorption experiments.
3.3. Characteristics of PTMF
The surface area and total pore volume of PTMF were determined using BET apparatus (Smart Instruments, Mumbai). The surface functional groups of PTMF were detected by Fourier transform infrared (FTIR) spectroscope (Shimadzu, Japan). About 150 mg KBr disks containing 2% of PTMF sample were prepared before recording the FTIR spectra in the range 450–4000 cm^{−1} with 16 cm^{−1} resolution.
The zero point charge was determined by suspending 1.0 g of the PTMF in 1 millimol/L NaNO_{3} solution for 24 h. Sixty milliliters of the suspension was measured into each of the eight conical flasks and the initial pH was adjusted to 2.14, 3.06, 4.1, 5.18, 6.14, 7.6, 8.48, and 9.22. The suspension in each of the flasks was divided into 4 equal parts and 0.3 g of NaNO_{3} was added to two sets, while the other pair contained no added nitrate. They were left for 6 h and after this the pHs of the reference and test suspensions were taken as initial and final pHs, respectively. The pairs containing no added nitrate were taken as the reference, while those with added nitrate were taken as the test samples [15]. The results were plotted as dpH against initial pH (pH_{f}).
3.4. Biosorption Experiment
3.4.1. Effect of pH
The effect of pH on amount of color removal was analyzed over a pH range of 2–9. The pH was adjusted using 0.1 N HCl and 0.1 N NaOH solutions. In this study 100 mL of dye solution of 200 mg/L was agitated with 0.3 g of PTMF powder at room temperature of 30°C. Agitation was carried out for 6 h which is more than sufficient to reach equilibrium at constant agitation of 150 rpm. The samples were then filtered and analyzed using double beam UV spectrophotometer (UV1700, Shimadzu, Japan) by monitoring the absorbance at a wavelength of maximum absorbance of 665 nm.
3.4.2. Biosorbent Dosage
The effect of PTMF concentration on the amount of color adsorbed was studied by dissolving various quantities (0.05, 0.1, 0.15, 0.2, 0.25, and 0.3 g) of biosorbent in 100 mL of dye solution of initial dye concentration of 200 mg/L. All the experiment was carried out at 30°C, pH of 6, and 150 rpm for 6 h.
3.4.3. Biosorption Equilibrium
The equilibrium experiments were carried out at 150 rpm by adding 0.3 g of PTMF powder to 100 mL dye solution. The dye concentration was varied from 50–300 mg/L. The amount of MB adsorbed per gram PTMF () was obtained using the following expression: where is the equilibrium uptake value (mg/g), is the sample volume (L), (mg/L) is the initial MB concentration, (mg/L) is the equilibrium MB concentration, and (g) is the dry weight of the PTMF powder. The percentage removal of the dye is given by
3.4.4. Biosorption Kinetics
Kinetic experiments were carried out by adding 0.3 g of PTMF powder to 100 mL of the dye solution at 30°C at an optimum pH of 6 and at 150 rpm. The dye concentration was varied from 50–200 mg/L. The amount of MB adsorbed per gram PTMF () was obtained using the following expression where (mg/g) is the uptake value at any time and (mg/L) is the liquidphase concentration at any time .
3.4.5. Effect of Initial MB Concentration
Equilibrium experiments were carried out by mixing 0.3 g of PTMF powder with 100 mL of MB solution of different initial dye concentration ranging from 50–300 mg/L. The studies were carried out at three temperatures (303 K, 313 K, and 323 K) using shaking incubator. After 6 h the samples were filtered and analyzed for residual MB. All experiments were carried out in duplicate under identical conditions and mean values are presented. The error obtained was 2.0–4.0%.
4. Results and Discussion
4.1. Characterization of Biosorbent
The BET surface area and total pore volume of PTMF were found to be 1.6 m^{2}/g and 2.8 m^{3}/g, respectively. Figure 2 shows the FTIR spectrum of PTMF biosorbent. The absorptions with maxima at 3440 cm^{−1} represent OH stretching of phenol group of cellulose and lignin and the band about 2924 cm^{−1} indicates presence of –CH_{2} stretching of aliphatic compound [16]. The peak at 2300 cm^{−1} is due to NH stretch. The band observed at 1744 cm^{−1} was assigned to a C=O stretching of aldehyde [16], while the peak at 1628 cm^{−1} was attributed to C=C stretching of phenol group [17]. The band at 1520 cm^{−1} was due to secondary amine group [18]. The band at 1458 cm^{−1} was due to aromatic ring of lignin. The band in 1258 cm^{−1} was due to bending modes of O–C–H, C–C–H, and C–O–H. The band at 1033 cm^{−1} was assigned to C–O stretching which confirmed the presence of lignin in PTMF [17]. The FTIR spectrum of palm tree male flower displays a number of absorption peaks, indicating the complex nature of the biosorbent (Figure 2). As seen from Figure 3 and Table 1, the spectral analysis before and after dye adsorption indicated that –OH group and other groups could be potential sites involved in MB adsorption.

4.2. Effect of pH on Biosorption of MB Dye
Effect of pH on MB removal is shown in Figure 4. The removal of MB increased with the increase in pH of solution from 2 upto 6. A decrease of 5.87% dye removal was observed in the pH range of 6–9. This could be attributed to solubilization of organic groups present on the biosorbent [17]. The pH at the point of zero charge, pH_{pzc} value of PTMF, was found to be 2.74 (Figure 5). At pH < pH_{pzc}, the PTMF surface may get positively charged due to adsorption of the H^{+} and a force of repulsion occurs between the dye cation and the biosorbent surface. Also, H^{+} concentration is high at lower pH due to which there is a competition for vacant adsorption sites between H^{+} and positively charged MB cation. This leads to lowering of the adsorption capacity.
At solution of pH > pH_{pzc}, the surface of PTMF may get negatively charged due to adsorption of OH^{−}, and the adsorption process is highly favored through electrostatic force of attraction. Similar trends were observed by various authors for MB adsorption on tea waste in [18], various carbon adsorbents in [9], peanut shell hull in [7], and phoenix tree leaves in [19]. At pH 6, surface of biosorbent was negatively charged to its maximum extent. Further increase in pH did not increase surface charge intensity as well as adsorption capability. Therefore, pH 6 was used for adsorption studies.
4.3. Effect of Biosorbent Mass
From Figure 6, it is evident that the MB sorption increases as biosorbent dose increases. The sorption rate increased from 40.75 to 91.65% at equilibrium as PTMF dose was increased from 0.05 to 0.30 g. This was attributed to increase in the biosorbent concentration, which increased the available surface area and the sorption sites [20]. But the sorption capacity decreased with the increase in biosorbent dosage. As the biosorbent dose was increased from 0.05 to 0.3 g the sorption capacity for PTMF decreased from 163 to 61.1 mg/g. This may be due to overlapping of sorption sites as a result of overcrowding of biosorbent particles [21].
4.4. Effect of Biosorption Equilibrium
The adsorption isotherm indicates how the adsorbed molecules distribute between the liquid phase and the solid phase when the adsorption process reaches an equilibrium state. The analysis of the isotherm data by fitting them to different isotherm models is an important step to find suitable model that can be used for design purpose [22].
The Langmuir equation is valid for monolayer sorption onto a surface with finite number of identical sites given by the following equation: where (mg/g) is the maximum amount of dye adsorbed per unit mass of biosorbent corresponding to complete coverage of the adsorption sites and (L/mg) is the Langmuir constant related to energy of adsorption. The linearized equation of Langmuir is represented as follows: A plot of versus (Figure 7) yields a straight line with slope and intercept values which are used to calculate and , respectively. The equilibrium data were fitted to Langmuir isotherm and the constant together with values is listed in Table 3.
The essential characteristics of the Langmuir isotherm can be expressed in terms of a dimensionless constant separation factor that is given by the following equation [23]: where (mg/L) is the highest initial concentration of adsorbate. The value of indicates the shape of the isotherm to be either unfavorable (), linear (), favorable (), or irreversible (). For the adsorption of MB onto PTMF, the values obtained are shown in Table 2 and Figure 8. The values for adsorption of MB onto PTMF are in the range of 0.07 to 0.3125 at 303 K, 0.058 to 0.27 at 313 K, and 0.055 to 0.26 at 323 K, indicating that the adsorption is a favorable process.


The Fruendlich isotherm [24] is an empirical equation assuming that the adsorption process takes place on heterogeneous surfaces and the adsorption capacity is related to the concentration of MB dye at equilibrium by where (mg/gL/mg) is roughly an indicator of the adsorption capacity and is the adsorption intensity. The magnitude of the exponent, , gives the indication of the favorability of adsorption. The linear form of Freundlich’s expression can be obtained by taking the logarithm of (see (16)) given by The plot of against (Figure 9) yields a straight line with slope and intercept values which are used to calculate and , respectively. The equilibrium data were fitted to Freundlich isotherm and the constants together with values are listed in Table 3. From the table, values of varies from 1.47 to 1.52 when the temperature vary from 303 to 323 K indicating favorable adsorption system.
Tempkin and Pyzhev [25] studied the heat of adsorption and adsorbentadsorbate interaction on the surfaces. The Tempkin isotherm is given by or where , (K) is the absolute temperature, and (8.314 KJ/Kmol K) is the universal gas constant. (L/mg) is equilibrium binding constant and (KJ/mol) is the variation of adsorption energy. A linear form of (19) can be expressed by A plot of versus (Figure 10) enables one to determine the constants and . The values of Tempkin constant and correlation coefficient, , are listed in Table 3. The values are lower than Freundlich and Langmuir values.
Generalized adsorption isotherm in [26] has been used in the following form: A linear form of this equation is given by where (mg/L) is saturation constant, is the cooperative binding constant, (mg/g) is the maximum adsorption capacity of biosorbent, and (mg/g) and (mg/L) are the equilibrium dye concentration in the solid and liquid phase, respectively. A plot of equilibrium data in the form of versus (Figure 11) gives constant and . The values were taken from Langmuir isotherm. The slope and the intercept of the best fit line are presented in Table 3. The values of correlation coefficient are much higher than Fruendlich and Tempkin isotherm values.
As shown in Table 3, the Langmuir equation represents the biosorption process very well; the values were higher than 0.997, indicating a very good mathematical fit. The fact that Langmuir isotherm fits the experimental data very well may be due to homogenous distribution of active sites on the PTMF surface, since the Langmuir equation assumes that the surface is homogenous. A comparison between the adsorption capacities of PTMF and other adsorbents is presented in Table 4. When comparing our results for PTMF with the results of others, it can be concluded that the PTMF has adsorbed MB dye as effective as other adsorbents listed.

4.5. Biosorption Kinetics
Figure 12 shows the effect of initial dye concentration on the rate of MB dye uptake onto PTMF. It is evident that the amount of dye adsorbed gets increased with the increasing dye concentration and contact time. It is also observed that the rate of MB uptake was found to be very rapid for the initial contact period of 45 to 60 min and thereafter the dye uptake rate slowed down and finally reached saturation. The higher sorption rate at the initial period may be due to more number of vacant sites available at the initial stages; as a result there exist increased concentration gradients between MB in solution and the MB in the PTMF surface. As time progresses, this concentration is reduced due to accumulation of MB particles in the vacant sites, leading to a decrease in sorption rate at a later stage.
The rate constant of adsorption is determined from the linear pseudofirstorder rate expression given by Lagergren in [35] in the following form: where and are amounts of dye adsorbed (mg/g) at equilibrium and at time (min), respectively, and (min^{−1}) is the rate constant of adsorption. Values of were calculated from the plot of versus (Figure 13). The calculated values of and and the corresponding linear regression correlation coefficient () are shown in Table 5. The values show that the pseudofirstorder model is not good in predicting the kinetics of MB adsorption onto PTMF.

The kinetic data were further analyzed using Ho’s pseudosecondorder kinetics represented by in [36] where (g/mg·min) is the rate constant of pseudosecondorder adsorption. If the secondorder kinetics is applicable, then the plot of versus should be a linear relationship. The initial adsorption rate, (mg/g·min), as can be defined as . The initial adsorption rate (), the equilibrium adsorption capacity (), and the secondorder constant () can be determined experimentally from the slope and intercept of plot versus (Figure 14) and the values are shown in Table 5. Calculated correlation coefficient () is closer to unity and its equilibrium adsorption capacity, (calculated), is consistent with experimental data. These facts suggest that the pseudosecondorder kinetic mechanism is predominant and that the overall rate of dye adsorption process appears to be controlled by chemisorption process [4]. Similar phenomena have been observed in the sorption of MB onto rice husk in [4], removal of MB from perlite in [37, 38], removal of MB from guava leaf powder in [10], adsorption of MB onto wheat shell in [5], activated carbon prepared from rattan sawdust in [39], and spent tea leaves in [28].
The half adsorption time of dye that is the time required for PTMF to uptake half the amount adsorbed at equilibrium is often considered as a measure of rate of adsorption and for the secondorder process is given by the following relation [40]: The determined values for for the tested parameters are given in Table 5.
4.6. Intraparticle Diffusion
The models mentioned above in adsorption kinetics cannot identify a diffusion mechanism. The adsorbate species are most probably transported from the bulk of the solution into the solid phase through an intraparticle diffusion process, which is often the rate limiting step in many adsorption processes. The possibility of intraparticle diffusion model based on Weber and Morris [40] was also tested. It is an empirically found functional relationship common to most adsorption processes, where uptake varies almost proportional with rather than with the contact time . According to this theory, where (mg/g·min^{1/2}), the intraparticle diffusion rate constant, is obtained from the slope of straight line of versus (Figure 15). The values of , , and correlation coefficient () obtained from plots are given in Table 6. The intercept gives an idea about the thickness of boundary layer that is the larger the intercept, the greater the boundary layer effect. If intraparticle diffusion occurs, then plot of versus will be linear and if the plot passes through the origin, then the rate limiting process is only due to intraparticle diffusion. Otherwise some other mechanisms along with intraparticle diffusion are also involved [29]. As it is shown Figure 15, the plot of versus consists of two linear sections with different slopes. A similar multilinearity has been observed with MB adsorption on sepolite in [29] cyclodextrin in [41]. The multilinearity indicates that two or more steps occur in the sorption process. The two linear sections in plot were evaluated separately using (26) and the model parameters are listed in Table 6.

4.7. Estimation of Thermodynamics Parameters
The free energy of adsorption, , can be related to equilibrium constant (L/mol) corresponding to the reciprocal of the Langmuir constant, by the following [42]: where (8.314 J/mol K) is the universal gas constant and (K) is absolute temperature. Also the enthalpy () and entropy () changes can be estimated by the following equation: Thus a plot of versus (Figure 16) should be a straight line. and values were obtained from the slope and intercept of the plot, respectively. , , and obtained from (27) and (28) are given in Table 7. The equilibrium constants obtained from Langmuir model at 303, 313, and 323 K were used to determine Gibbs free energy changes. The plot of versus had a very good linearity with regression coefficient of 0.9972. The value increased with increasing temperature which resulted in a shift of adsorption to the right. The Gibbs free energy values for adsorption process were obtained as −24.06, −25.4, and −26.34 KJ/mol for temperatures of 303, 313, and 323 K, respectively. The negative value of indicates the spontaneous nature of MB adsorption onto PTMF. According to (28), the enthalpy and entropy values in the range of 303–323 K were obtained as 15.06 KJ/mol and 0.129 KJ/mol K, respectively. The positive value of indicates that the adsorption is an endothermic process. The increase in temperature would increase the rate of diffusion of the adsorbate molecules across the external boundary layer and also in the internal pores of biosorbent particles, owing to the decrease in viscosity of solution [43]. The positive value of showed the increase in randomness at the solidsolution interface during adsorption.

4.8. Mathematical Model
The equilibrium data were approximated by Langmuir isotherm. The linear regression analysis was employed to determine isotherm constants and . The estimated isotherm constants at temperature of 30°C are =145 mg/g and = 0.044 and correlation coefficient is 0.9999 which indicates a satisfactory description of equilibrium data by isotherm model. Figures 17, 18, 19, and 20 show the experimental decaytime profile of MB adsorption onto PTMF at different initial solute concentration. As shown, the mentioned model describes well the experimental data. The correlation coefficients for all experiments were computed and reported in Table 8. All correlation coefficient are in excess of 0.99, indicating satisfactory fit of model prediction and experimental data. The estimated values of and are m^{2}/s and m/s, respectively.

5. Conclusions
The present study shows that PTMF, a plant waste material, can be used as a potential biosorbent for removal of MB from aqueous solution. The amount of dye adsorbed was found to vary with biosorbent dosage, initial dye concentration, and pH and temperature. The amount of dye uptake (mg/g) was found to increase with temperature and initial dye concentration but decreased with increase in biosorbent dosage. The rate of adsorption was found to conform to pseudosecondorder kinetics with a very good correlation coefficient. Equilibrium data fitted very well with the Langmuir isotherm equation and generalized isotherm confirming the monolayer adsorption capacity of MB onto PTMF with a monolayer adsorption capacity of 157.3 mg/g at 323 K. The dimensionless separation factor () showed that PTMF can be used for removal of MB from aqueous solutions. The thermodynamic parameters indicate spontaneous and endothermic process. The mathematical model derived gave a satisfactory fit of model prediction and experimental data thereby indicating that the adsorption is only taking place on the surface of the PTMF with negligible intraparticle diffusion. PTMF, an inexpensive and abundantly available material, can be used as an alternative for more costly adsorbents used for dye removal in waste water treatment.
The disposal of biosorbent loaded with dye must be evaluated so as to ensure environmentally safe conditions. The following disposal options may be considered: (i) burning after drying and the heat used for steam generation; (ii) use of composite materials; (iii) composting process of biodegradable wastes; (iv) regeneration by treatment with acid or organic solvent solution and reuse in other cycle of biosorption [44].
Greek Symbol
Φ:  solid loading (kg/m3 of liquid). 
Conflict of Interests
The authors declare that there is no conflict of interests regarding the publication of this paper.
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Copyright © 2014 M. Srinivas Kini et al. This is an open access article distributed under the Creative Commons Attribution License, which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited.