Potential Biosorbent Derived from Calligonum polygonoides for Removal of Methylene Blue Dye from Aqueous Solution
The ash of C. polygonoides (locally called balanza) was collected from Lakki Marwat, Khyber Pakhtunkhwa, Pakistan, and was utilized as biosorbent for methylene blue (MB) removal from aqueous solution. The ash was used as biosorbent without any physical or chemical treatment. The biosorbent was characterized by using various techniques such as Fourier transform infrared spectroscopy (FTIR), thermogravimetric analysis (TGA), and scanning electron microscopy (SEM). The particle size and surface area were measured using particle size analyzer and Brunauer-Emmett-Teller equation (BET), respectively. The SEM and BET results expressed that the adsorbent has porous nature. Effects of various conditions such as initial concentration of methylene blue (MB), initial pH, contact time, dosage of biosorbent, and stirring rate were also investigated for the adsorption process. The rate of the adsorption of MB on biomass sample was fast, and equilibrium has been achieved within 1 hour. The kinetics of MB adsorption on biosorbent was studied by pseudo-first- and pseudo-second-order kinetic models and the pseudo-second-order has better mathematical fit with correlation coefficient value () of 0.999. The study revealed that C. polygonoides ash proved to be an effective, alternative, inexpensive, and environmentally benign biosorbent for MB removal from aqueous solution.
Environmental pollution is a serious and challenging problem all over the world because of the rapid progress in society, science, technology, and industries. The industrial effluent containing both inorganic and organic toxic material which discharging into surface water that seriously affect biodiversity, ecosystem functioning and natural activities of aquatic system. Among these pollutants one such pollutant is the synthetic dyes which are considered to be the most common and toxic water pollutants [1–5]. The dye compounds have been extensively used in various industries to colorize the products, such as in papers and pulp, textiles, plastics, wool, paints, rubber manufacturing, printing, cottons, cosmetic products, foods, and pharmaceuticals. The extensive use of dyes and dyes containing compounds disturb the aquatic system by inhibiting the sunlight from reaching water and thus reducing photosynthesis and increasing the biological oxygen demand (BOD) and chemical oxygen demand (COD) values [1–3, 5]. Among these dyes some cause depletion of the dissolved oxygen content of water thus affecting aquatic life badly. In addition, certain textile dyes are carcinogenic and toxic to living organisms and have adverse effect on human health, domestic animals, and wildlife .
Among the dyeing agents, methylene blue (MB) which is a heterocyclic aromatic chemical compound is widely used in the textile industries [6–9]. MB and MB like other textile dyes can cause eye burns in humans and animals, skin irritation, dyspnea, convulsions, cyanosis, tachycardia, and dyspnea, and if ingested can cause gastrointestinal tract irritation, nausea, vomiting, also diarrhea, and so forth [10–12]. Due to these toxicological and hazardous effects of dyes on environment and subsequently on living organism, the removal of these dyes from wastewater is a key challenging task for researchers and an important area of research directed towards a better life [10, 13–15].
There are various physical and chemical methods used for removal of textile dyes from aqueous media. These include ion exchange, membrane filtration, electrochemical destruction, ozonation, flotation, chemical coagulation, biological and chemical oxidation, precipitation, and electrokinetic and adsorption methods [16–19]. However most of these methods have some major drawbacks, such as the applicability at relative high concentration of dye, insufficient dye removal, high cost and production of extra waste . Similarly, the biological methods often demand a very strict control of experimental conditions and especially the pH and the decontamination process is usually very slow. Alike, in chemical oxidation methods, the biodegradation products are often carcinogenic and toxic in nature which affects the aquatic life.
Activated carbon has been extensively used as an adsorbent for the removal of dyes because of the acidic nature and showed pores nature of its surface [21–23]. However, the activated carbon is costly and challenging in regeneration which raises the cost of waste water treatment [24, 25]. Thus, there is a great demand for such type of adsorbent which is cheaper and still has high adsorption capability towards pollutants and dyes without any additional expensive pretreatment. Presently cellulose and lignocellulosic biomass have got considerable attraction because of the abundance, effectiveness, low cost, and environmentally friendly nature of these biopolymers. Thus biosorption has been proved to be the most effective technique for the removal of MB from the aqueous solution [16, 26–29].
In this research work C. polygonoides (locally called balanza, which is used as fuel for domestic cooking purposes and in bricks kiln industry) was collected from Lakki Marwat, Khyber Pakhtunkhwa, Pakistan, and utilized as biosorbent for MB removal from aqueous solution without any physical or chemical treatment. The utilization of this alternative, abundant, low cost, and environment friendly bioadsorbent will effectively reduce both the waste disposal problem and the cost of waste decontamination.
2. Materials and Methods
2.1. Methylene Blue
All the chemicals used in the present research work were of analytical grade and purchased from Sigma-Aldrich, BDH, and Merck. MB with chemical formula C16H18ClN3S3H2O (Table 1) was used as model adsorbent to study the adsorption capacity of biosorbent. The stock solution of 1000 ppm of MB was prepared and subsequently their solutions of desired concentration were prepared by applying the dilution formula ().
2.2. Preparation of Biosorbent
The Calligonum polygonoides ash was washed with double distilled water to remove soluble impurities and then dried in oven at 110°C for 5 hours. The powdered material thus obtained was sieved through 45 μm sieve using Retsch AS 200 basic and was stored in air tight glass bottle for further experimental study (Figure 1).
2.3. Characterization of Biosorbent
2.3.1. Scanning Electronic Microscopic (SEM) Analysis
The surface structure of biosorbent was analyzed using scanning electron microscopy (JMT-300, JEOL).
2.3.2. Surface Area Analysis
The surface area of C. polygonoides ash sample was determined using Brunauer-Emmett-Teller (BET) method and the pore size diameter was obtained by BJH method from the adsorption/desorption isotherm of nitrogen gas, at 77.0 K, employing Micromeritics ASAP 2010 apparatus.
2.3.3. Fourier Transform Infrared Spectroscopy
The chemical structure and nature of functional groups C. polygonoides ash were studied using FTIR transmission spectra on a Perkin Elmer Spectrum One. For FTIR spectra measurement, sample was mixed with KBr in the ratio of 1/1000 and pressed into the pellet using a Perkin Elmer hydraulic pump. FTIR spectrum was recorded in the wave number range from 4000 to 450 cm−1 with resolution of 5 cm−1.
2.3.4. TGA Analysis
To investigate the thermal characteristic or weight-loss profiles of C. polygonoides ash, a thermogravimetric analyzer (Pyris-1, Perkin Elmer, Shelton, CT) was used over the temperature range from 50°C to 800°C at heating rate 10°C/min. The analysis was conducted under N2 gas with flow rate of 50 mL/min and weight of samples taken was around 5–7 mg.
2.3.5. Particle Size Analysis
The particle size distributions were measured using Mastersizer 2000 ver. 5.54, serial number: Mal 18486 (Malvern Ltd., UK). For particles size distribution measurement, 0.5 g of C. polygonoides ash was loaded into the tray and dispersed by compress air to bring sample into laser beam for measurement of the particle size distributions.
2.4. Experiments for Dye Adsorption
The biosorption experiment of MB was conducted by adding 100 mg of biosorbent to 25 mL of aqueous solution of MB dye (4–10 mg/L) in 50 mL of conical flask and shaken at 300 rpm in orbital shaker at 298 K. After specific interval of time, sample aliquots were withdrawn and centrifuged to separate the dye loaded from dye solution. The remaining concentration of MB was measured spectrophotometrically by measuring the absorbance of the supernatant (dye solution) left after centrifugation. To find the optimum experimental conditions for MB removal, for MB removal, the effect of time (10–120 min), initial dye concentration (2 mg/L–10 mg/L), biosorbent loading (20–100 mg), and shaking velocity (100–600 rpm) were thoroughly studied.
The color removal efficiency () and adsorption capacity of C. polygonoides ash were measured by applying the following equations: where and (mg/g) are the amount of MB adsorbed at time and equilibrium, respectively; , , and (mg/L) are concentration of MB at initial, time , and equilibrium, respectively; is the solution volume and (g) is the mass of biosorbent.
2.5. Kinetic Study and Model Fitting
To study the adsorption mechanism of MB on biosorbent pseudo-first- and pseudo-second-order kinetic models were used.
2.5.1. The Pseudo-First-Order Equation
The pseudo-first-order kinetic model or Lagergren kinetic equation is generally expressed as follows: where is the amounts adsorbed (mg/g) at equilibrium, is the amounts adsorbed (mg/g) at any time, and is the adsorption rate constant for pseudo-first-order ().
2.5.2. The Pseudo-Second-Order Model
If the rate of sorption is a second-order mechanism, the pseudo-second-order kinetic rate equation is used and it is expressed as By integration of (3) for the boundary conditions when and where (g/mg·min) is the rate constant of pseudo-second-order: If is plotted against , it gives a straight line, which means that the adsorption follows pseudo-second-order kinetics. This model is based upon the assumption, if the rate limiting step may be chemisorption which involve valence forces due to the electron sharing or exchange of electron between the adsorbent and adsorbate.
3. Results and Discussion
3.1. Particle Size Distributions
After thermal treatment, the particle size of adsorbent decreases. Decrease in particles size of adsorbent usually results in enhanced adsorption of dye because the adsorption capacity of the adsorbent is directly proportional to the exposed surface area and inversely related to the particle diameter of nonporous material . By increasing the particle size, the number of particles per given mass decreases which results in decrease in specific surface area and hence the adsorption capacity. The particle size distribution of pure C. polygonoides powder changed from (0.1) 12.39 μm, (0.5) 120.79 μm, and (0.9) 480.309 μm to (0.1) 2.36 μm, (0.5) 27.90 μm, and (0.9) 382.84 μm, respectively, after burning. The C. polygonoides ash sample becomes black in color with some gray particles, resulting from different stages of carbon combustion during burning process of the biomass. The amount of black particles decreases with increasing the calcination time and temperature.
3.2. Surface Area (BET)
The process of adsorption is a multistep complex phenomenon and therefore many factors affect the phenomenon. Among these factors, the pore size of adsorbent significantly affects the adsorption process. Pores size is generally classified into various groups such as micropores (<2 nm diameter), mesopores (2–50 nm), and macropores (>50 nm). The surface chemistry of adsorbent and its pores structure considerably affect the adsorption of big molecules like MB into its structure. MB has molecular cross-sectional diameter of about 0.8 nm and cannot easily penetrate material with pores smaller than 1.3 nm. The surface area of C. polygonoides ash depends on the amorphous carbon content. During the dye adsorption process, the diffusion of dye molecules to the active sites takes place first, which is followed by attachment of these dye molecules to the active sites. The pore size and total pore volume thus play a decisive role in the adsorption process.
C. polygonoides ash has significant surface area and wide pore size distribution. The BET surface area of C. polygonoides ash is 4.3810 m2/g, whereas BJH adsorption/desorption surface area of pores of C. polygonoides ash is 4.119/4.7108 m2/g. For C. polygonoides ash the single point total pore volume of pores () is found to be 0.016691 cm3/g. The cumulative adsorption/desorption pore volume of the pores ) of C. polygonoides ash is 0.019823/.019556 cm3/g (Table 2). The C. polygonoides ash, thus, is found to consist of mesopores predominantly. This is what is desirable for the liquid phase adsorptive removal of metal ions and dyes.
3.3. Fourier Transform Infrared Spectroscopy
It is important to know the exact chemical structure of the adsorbent in order to understand the adsorption process. FTIR spectroscopy was thus employed to characterize the chemical structure of C. polygonoides before and after thermal treatment (Figure 2). The broad band around 3400 cm−1 can be assigned to the stretching vibration of O–H and N–H groups. This peak is broad because of the complex vibrational modes due to participation of –OH group in hydrogen bonding. This peak represents the presence of hydroxyl group and chemisorbed water in the adsorbent [43, 44]. Beside this, the vibrational modes in this area also correspond to inter- and intramolecular hydrogen bonding. The presence of a peak at 2910 cm−1 shows the symmetric and asymmetric C–H stretching due to the existence of methyl and/or methylene groups . The peak located at 1380 cm−1 is indicative of –CH3 group. The sharp intense peak at about 1637 cm−1 corresponds to O–H bending vibration of secondary adsorbed water molecules. The bands at 1528 and 1445 cm−1 confirm the presence of C=C bond of alkene and aromatic ring . The FTIR spectra showed the presence of another peak at 1100 cm−1 which may tentatively be assigned to Si–O–Si and –C–O–H stretching and –OH deformation. The absorption peaks in region from 1000 to 1200 cm−1 represented the main skeleton of cellulose. The presence of peak at 1035 cm−1 represents stretching vibration of cellulose/hemicellulose and ary-OH group in lignin. The presence of polar groups on the surface is likely to give considerable cation exchange capacity to the adsorbents. The occurrence of peaks at about 793 shows the existence of Si–H . The presence of adsorption band in region from 1300 to 900 cm−1 represents the carbonyl component (i.e., alcohols, esters, carboxylic acid, or ethers) [16, 47]. The presence of absorbance peaks in region from 900 cm−1 shows O–H stretching vibrations which represented aromatic groups. In C. polygonoides ash, the peak (900 cm−1) of secondary adsorbed water is not present because of thermal treatment. The appearance of peak at 3700 cm−1 in C. polygonoides ash is related to stretching of free O–H functional group . The presence of polar groups on the surface is likely to give considerable cation exchange capacity to the adsorbents.
3.4. Morphology of Adsorbent
Scanning electronic microscopy (SEM) study is one the most popular, primary, and widely used characterization techniques applied for the study of surface properties and morphology of biosorbent material. Moreover, SEM study also tells about porosity and texture of biosorbent material [25, 44, 48, 49]. Figure 3 shows that C. polygonoides ash has small cavities on surface and has a porous texture that may provide large surface for the adsorption of the dye molecules.
3.5. Thermogravimetric Analysis
Thermogravimetric analysis (TGA) is an important analytical technique used to study the thermal characteristics of carbonaceous materials. The TGA provide information on the degradation process of material occurring at different temperatures and under different atmosphere.
The C. polygonoides ash was subjected to TGA under argon atmosphere. Figures 4(a) and 4(b) show the TGA and differential thermal analysis (DTA) curves for C. polygonoides ash, respectively. TGA result of C. polygonoides ash shows a typical three-stage mass loss.(i)The first mass decomposition occurred below 100°C, which could attribute to water elimination/desorption which are physically absorbed in C. polygonoides ash. The DTA graph also shows an endothermic peak at 100°C. In this region the loss of very small amount of volatile compounds may also be contributed to the weight loss.(ii)The second mass loss which appeared around 300°C is due to the thermal decomposition of cellulose/hemicellulose/lignin degradation.(iii)The third mass decomposition occurred between 350 and 550°C, corresponding to the burning of carbonaceous residues .
4. Optimizations of Parameters
4.1. Effect of Contact Time and Initial Concentration of Dye
The time of contact between the dye and adsorbent and also the concentration of dye can affect the adsorption process. Figures 5(a) and 5(b) show adsorption with respect to contact time and initial concentration of MB on the surface of C. polygonoides ash, respectively. The % removal efficiency and adsorption capacity of MB increased with increase of contact time and reached equilibrium after 60 min. Increase in contact time after 60 min cannot enhance the adsorption of MB on C. polygonoides ash . In the beginning, the % removal of dye is very rapid due to the adsorption of more molecules of dye on the unsaturated external surface of adsorbent. After 60 min the surface pores of adsorbent are covered and it becomes difficult for dyes molecule to enter into the interior of adsorbent. The initial rapid % removal of dye may be due presence of more binding sites for adsorption of dye molecules and the slow removal of dye in the last stages may be due to occupation/saturation of these binding sites with dyes molecules . The equilibrium time required for the adsorption of different dye concentration is independent of their initial concentration. The result shows that for all of the initial concentration the equilibrium was reached in the same time. Khattri and Sing also obtained the same observation during adsorption of MG on neem sawdust [35, 44, 50]. It was found that with increase of the concentration of dye from 4 to 10 mg/L the rate of adsorption and thus % removal and adsorption capacity increase. It is very common practice in the adsorption of dyes molecules that with increase of initial concentration of dyes the capacity of adsorption increases because of strong driving force and transfers of more dye molecules from aqueous phase to solid phase increase .
Tables 3(a) and 3(b) show a comparison of % removal and adsorption capacity of C. polygonoides ash with that of other adsorbents reported in the literature. It becomes clear that the adsorption capacity of the C. polygonoides ash is higher than many of the reported adsorbents.
4.2. Effect of Shaking Speed
To investigate the effect of stirring speed on the adsorption of MB on C. polygonoides ash, the experiments were carried using different stirring speed from 100 to 600 using dye concentration of 10 mg/L, contact time was 60 min, and the temperature was 298 K. Figure 6 shows the effect of shaking speed on the MB adsorption. With increasing of the shaking speed the adsorption or % removal of dye from aqueous solution was increased. This increase in adsorption reached a maximum at 300 rpm and after this there is no such considerable increase in the adsorption of dyes. This increase in adsorption reached a maximum at 300 rpm and, further increase in speed had no significant effect on the adsorption of the dye. The increase in adsorption of MB may be to the decrease in the thickness of diffuse layer around the surface of adsorbent with increasing the stirring speed .
4.3. Effect of Adsorbent Dose
The amount of adsorbent greatly affects the removal of dye from aqueous solution. The effect of C. polygonoides ash amount on MB adsorption was investigated in the range from 20 mg to 100 mg. Figure 7 shows that with increase of C. polygonoides ash amount, the % adsorption capacity of MB is increased . This increase in adsorption of MB with the increase of C. polygonoides ash amount is due to the increase in the availability of more and more surface area and active sites. Similarly by increasing the surface area more and more adsorption pores are available for MB adsorption . Further increase in concentration of both C. polygonoides ash beyond 100 mg the adsorption of MB cannot increase; this may be due to saturation of vacant spaces or the aggregation/agglomeration of biosorbent particles with each other. In the present study therefore 100 mg of C. polygonoides ash was optimized. Similar results have been reported by other researchers for other dye adsorptions .
4.4. Kinetics of Adsorption and Model Fittings
The adsorption mechanism process of MB on C. polygonoides ash was evaluated by using pseudo-first-order and pseudo-second-order kinetic models  (Table 4). From Figure 8 and Tables 5 and 6 it is clear that the adsorption of MB on C. polygonoides can be fitted in the pseudo-second-order kinetics with regression coefficient () 0.999.
4.5. Intraparticle and Liquid Film Diffusion Model
The diffusivity of the solute molecules plays an important role in the determination of overall rate of an adsorption process. Although the pseudo-second-order equation was found to the best fitted order for present experimental data, the results obtained from this model are not sufficient to predict the diffusion mechanism. During a solid/liquid adsorption process, adsorbate transfer was usually governed by liquid phase mass transport (boundary-layer diffusion), or intraparticle mass diffusion, or both. The slowest step, which might be either film diffusion or pore diffusion, would obviously be the overall rate-controlling step of the adsorption process. The intraparticle and liquid film diffusion models are represented by Figure 9 shows the interparticle diffusion model fitting for the adsorption of various concentration of MB. The result shows that the plot of versus is not very linear for whole time and can be divided into two regions. The multilinearity of the plot for MB adsorption shows the multistage adsorption of MB on the C. polygonoides. Normally if the plot of versus passed through origin this indicates the interparticle diffusion is only the rate limiting step. However in this study it is clear that the plot of versus is not passing through the origin, which shows that the intraparticle diffusion is not involved in the adsorption process; therefore it is not a sole rate-controlling step. This result confirms that the adsorption process is followed by two or more than two phases [4, 56].
In the first region the plot is linear due to mass transfer, which allows the MB molecules to be transported to the external surface of biomass through film diffusion. In this portion the adsorption is very first because of the strong interaction between the MB molecules and the external surface of the adsorbent.
After boundary-layer diffusion, the MB molecules entered through pores to the interior of the biomass by intraparticle diffusion, as reflected by the second linear portion of the plot. The stage of gradual adsorption whose rate was controlled by intraparticle diffusion was followed by a final equilibrium stage during which the intraparticle diffusion started to slow and become stagnant as the adsorbate molecules occupied all of the active sites of the adsorbent and the maximum adsorption was attained. Although all of the intraparticle diffusion plots for different initial dye concentrations provided a linear relationship, none of the line segments passed through the origin. The nonzero intercepts of the plots indicate that intraparticle diffusion is involved in the adsorption process but is not the sole rate-controlling step for the adsorption of MB. The increment of with increasing initial MB concentration simplifies that the increased driving force at high initial concentrations promotes intraparticle diffusion of the adsorbate onto the adsorbent.
4.6. Adsorption Mechanism of Dye
The adsorption mechanism depends on the structure of dye molecule and also the surface of adsorbent. The MB is cationic dye having amine group in its structure formula and while dissolving in water its molecule dissociated into MB+ and Cl−1. The FTIR result shows that the C. polygonoides ash has –OH group which is more exposed and has strong chemical interaction between dye ions and adsorbent and interacts mechanically because of easy penetration of dye ions to the microstructure of adsorbent.
The mechanism for adsorption of MB on adsorbent may be involving the following major steps.
(a) Migration of Dye Molecules. In this step the passage of MB molecules from bulk of the solution occurred to the surface of the adsorbent.
(b) Diffusion of Dye Molecules. In this step the diffusion of dye molecules can take place through the boundary layer to the surface of the adsorbent.
(c) Adsorption of Dye Molecules. In this step there is formation of surface hydrogen bonding between the nitrogen atom of MB and hydroxyl group of C. polygonoides ash. Figure 10 shows the proposed possible mechanism for adsorption of MB molecules on the surface of C. polygonoides ash
(d) Intraparticle Diffusion of Dye. In this final step the dye molecules get approached inside the pores of adsorbent.
From this present research work the following main conclusions are investigated.
C. polygonoides ash is proved to be the promising biosorbent for removal of MB from aqueous solution. The percentage of removal of dye on these biosorbents is fast and adsorption equilibrium is achieved in about 60 min. More than 97% removal of MB was approached in first 60 min after that no increase in adsorption was taking place. Dye adsorption increased with the increase in the amount of adsorbate. The adsorption of MB on C. polygonoides ash adsorbent followed the pseudo-second-order kinetics models which are indicated by correlation coefficient values. A comparison of adsorption capacity of C. polygonoides ash with many other biosorbents reported in the literature indicates far better performance of C. polygonoides. Due to its low cost, high adsorption capacity, and environmentally friendly nature, C. polygonoides ash could be used as a promising adsorbent in future for effective large scale removal of MB from aqueous solution on a large scale.
Conflict of Interests
The authors declare that there is no conflict of interests regarding the publication of this paper.
The authors acknowledge the Department of Chemistry, University of Science and Technology, Bannu 28100, Khyber Pakhtunkhwa, Pakistan, for supporting this research work and also thankful to the Deanship of Scientific Research, King Saud University, Riyadh, for funding the work through the collaborative research work with research group Project no. RGP-210.
Figure 1: Particle size analysis.
Figure 2: Surface area (BET).
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