# Biosorption Potential ofTrichoderma gamsii Biomass for Removal of Cr(VI) from Electroplating Industrial Effluent

Authors: B. Kavita; Haresh Keharia
Journal: International Journal of Chemical Engineering
 (2012)

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## Abstract

The potential use of acid-treated biomass ofTrichoderma gamsii to remove hexavalent chromium ions from electroplating industrial effluent was evaluated. Electroplating industrial effluent contaminated with 5000 mg/L of Cr(VI) ions, collected from industrial estate of Gujarat, India, was mixed with acid-treated biomass of T. gamsii at biomass dose of 10 mg/mL. Effect of contact time and initial Cr(VI) ions was studied. The biosorption of Cr(VI) ions attained equilibrium at time interval of 240 minutes with maximum removal of 87% at preadjusted initial Cr(VI) concentration of 100 mg/L. The biosorption of Cr(VI) ions by biomass of T. gamsii increased as the initial Cr(VI) ion concentration of the effluent was adjusted in increasing range of 100–500 mg/L. At 500 mg/L, initial Cr(VI) concentration, acid-treated biomass of T. gamsii showed maximum biosorption capacity of 44.8 mg/g biomass from electroplating effluent. The Cr(VI) biosorption data were analysed using adsorption isotherms, that is, Freundlich and Langmuir isotherm. The correlation regression coefficients (R2) and isotherm constant values show that the biosorption process follows Freundlich isotherm (R2>0.9, n>1, and Kf=8.3). The kinetic study shows that biosorption of Cr(VI) ions by acid-treated biomass of T. gamsii follows pseudo-second-order rate of reaction at increasing concentration of Cr(VI).
In conclusion, acid-treated biomass of T. gamsii can be used as biosorbent for Cr(VI) ions removal from Cr(VI)-contaminated wastewater generated by industries.


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## Body

## 1. Introduction

Variety of anthropogenic sources including leather tanning, electroplating, wood preservation, metal finishing, pigment, and dye industries contribute towards hexavalent chromium in the environment [1–3]. The hexavalent chromium is classified in group A of human carcinogens by United State Environmental Agency (USEPA). Therefore, USEPA has regulated/limited the industrial discharge of Cr(VI) to surface water up to <0.05 mg/L.Many conventional methods including chemical precipitation, chemical coagulation, ion exchange, electrochemical methods, adsorption using activated carbon and natural zeolite, membrane process, and ultrafiltration have been employed by several industries to remove Cr(VI) from their effluent [4–6]. However, these methods suffer from several disadvantages which include high operating cost, excess production of sludge, decrease in removal efficiency in presence of other metals, and large consumption of chemicals [7]. Hence, remediation of Cr(VI) demands some cost effective, economic, efficient, and eco-friendly methods.In this context, biosorption is an emerging and attractive technology which is being worked out by many researchers since last two decades [8–10]. In general fungal cell walls are mainly 80–90% polysaccharides, with proteins, lipids, polyphosphates, and inorganic ions. Chitin is a common constituent of fungal cell walls. Chitin is a strong but flexible nitrogen containing polysaccharide consisting of N-acetyl-glucosamine residues. All these biopolymers offer many functional groups such as carboxyl, hydroxyl, sulphate, phosphate, and amino groups that can bind with several metal ions [11]. The ongoing research on Cr(VI) biosorption suggests that fungal biomass can passively bind metal ions via various physicochemical mechanisms or combination of several phenomena, namely, ion exchange, complexation, coordination, adsorption, electrostatic interaction, and chelation [12, 13]. For example, biosorption of Cr(VI) by using Rhizopus arrhizuswas found to be 23 mg/g biomass [14]. Similarly several other biomasses of fungal origin have been reported extensively for Cr(VI) biosorption (Table 1). The process of biosorption has gained importance over conventional methods due to several advantages like reusability of biomaterial, removal of heavy metal from effluent irrespective of toxicity, short operation time, and no secondary compound production [15]. However, reports on practical application of any of these biosorbents to Cr(VI) containing wastewater are sparse [13, 16].Table 1
Comparison of various fungal biomasses for Cr(VI) biosorption.
Fungal biosorbentsMaximum biosorption capacity (mg/g biomass)ReferenceAspergillussp.1.56[18]Rhizopus arrhizus8.40[19]Termitomyces clypeatus11.1[20]Aspergillus niger11.6[21]Rhizopus nigricans12.70[22]Neurospora crassa15.85[23]Rhizopus arrhizus23.2[24]Mucor hiemalis30.5[25]Electroplating is one of the metal finishing process which contributes in discharging toxic level of Cr(VI) in environment. Apart from Cr(VI), electroplating industrial effluent contains many other metal ions which may affect the Cr(VI) biosorption efficiency of biomass. Therefore, it is of key importance to investigate the biosorption efficiency of biomass in contaminated effluent and effect of other parameters of effluent on biosorption process.We have isolated a hexavalent chromium tolerant fungal culture, identified asT. gamsii, from a chromium contaminated soil. This isolate exhibited a very efficient biosorption capacity for hexavalent chromium from pure solutions (50.6 mg/g biomass). In the present study we have investigated the utility of T. gamsii biomass for removal of Cr(VI) from electroplating industrial effluent.


## 2. Materials and Methods

### 2.1. Chemicals and Fungal Strain

All the chemicals used were of analytical grade (AR) and purchased from either Qualigens Fine Chemicals, India, or Hi-Media Laboratories, India or Ranbaxy Fine Chemicals Limited, India.A laboratory Cr(VI) tolerant fungal strain designated as FCR16 was used for present studies. FCR16 was grown and maintained on Potato Dextrose liquid/solidified medium as per the requirement.FCR16 was identified by 18 s rDNA sequencing. The analysis of the nucleotide sequencing was carried out using Blast-n tool at NCBI (http://blast.ncbi.nlm.nih.gov/Blast.cgi). The phylogenetic tree was constructed by neighbour joining method using MEGA version 4.0 [17].


### 2.2. Preparation of Fungal Biomass for Cr(VI) Ion Biosorption

FCR16 was inoculated by transferring a block of fungal growth (16 mm diameter) on Potato Dextrose agar plates (grown for three days at 30°C) using sterile cup borer to 500 mL Erlenmeyer flasks filled with 200 mL of culture medium composed of the following (g/L): Potatoes infusion forms, 200; and Dextrose, 20 and incubated on to a rotary shaker at 150 rpm for five days at 30°C. Upon incubation, the biomass produced was separated by filtration and the resulting biomass was washed thoroughly for several times with distilled water. The biomass was treated with hydrochloric acid (6N), washed with distilled water to bring the pH of the biomass in neutral range, and then was used directly for Cr(VI) adsorption studies from electroplating industrial wastewater, considering the higher Cr(VI) biosorption capacity of acid-treated biomass of FCR16 in pure Cr(VI) solution.


### 2.3. Characteristics of Effluent Sample

Electroplating effluent was collected from an electroplating unit located in Industrial Estate of Vadodara, Makarpura, Gujarat, India. The characteristics of electroplating effluent are listed in Table2. The major contaminants of wastewater were Cr(VI), Ni, and Fe. In addition, pH of the waste water was highly acidic that is, 1.5.Table 2
Physical and chemical characteristics waste water collected from effluent of electroplating industry.
Parametersmg/LCOD32Ammonium nitrate61.6Total solids10.30Total dissolved salts10.1Chlorides350SulphateNDSulphidesNDNickel32.8Iron10.31Oil and grease10.66Hexavalent Cr(VI)5,000pH1.5ColorYellow to brown


### 2.4. Batch Experiment

The biomass (at biomass dose of 10 mg/mL) of FCR16 was mixed with 100 mL of diluted effluent containing Cr(VI) in the range from 100 to 500 mg/L. Apart from Cr(VI) concentration adjustments, no other pretreatment was given to the effluent. After mixing, the experimental set was kept on shaker (150 rpm) at 30°C. 1 mL sample was withdrawn at regular time interval and residual Cr(VI) was measured.


### 2.5. Kinetics of Cr(VI) Biosorption

Pseudo-first-order and pseudo-second-order rate equations have been used for modelling the kinetics of Cr(VI) ion biosorption [26]. Linear form of pseudo-first-order rate equation is expressed as follows:(1)log⁡(qeq-qt)=log⁡qeq-k1t2.303,
where qt and qeq are sorption capacity at time t and at equilibrium, respectively, and k1 is pseudo-first-order rate constant.In case the biosorption follows pseudo-first-order rate equation, a plot oflog(qeq-qt) versus t should generate straight line with intercept of logqeq and slope of -k1/2.303.Similarly, linear form of pseudo-second-order rate equation is expressed as(2)tqt=1k2(qeq)2+tqeq,
where k2 is pseudo-second-order rate constant.In case the biosorption follows pseudo-second-order rate equation, a plot oft/qt versus t should generate a straight line with intercept of 1/k2qeq2 and slope of 1/qeq.The shape (linearity) of graph and comparison of experimental and calculatedqeq values can help in deciding which kinetic model is followed by biosorption process. Another important factor which influences the kinetic model is the value of coefficient of determination: R2. A value of R2>0.9 shows the suitability of model for describing the kinetics.


### 2.6. Equilibrium Model for Cr(VI) Biosorption by FCR16 Biomass from Electroplating Wastewater

Biosorption data were analyzed using Langmuir and Freundlich equilibrium isotherms to determine the feasibility of Cr(VI) ion biosorption. The Freundlich isotherm equation is an empirical equation based on the biosorption on a heterogeneous surface suggesting that the binding sites are not equivalent or dependent [27]. Langmuir isotherm equation is based on monolayer sorption onto a surface with finite number of identical sites, which are homogeneously distributed over the sorbent surface [28].


### 2.7. Analysis of Cr(VI) Ions

The concentration of the Cr(VI) ions was determined spectrophotometrically after complexation of the Cr(VI) with 1, 5-diphenylcarbazide [29]. The absorbance was recorded at 540 nm and concentration was determined from the calibration curve.Characterization of effluent was done according to standard methods described by APHA [30].


## 2.1. Chemicals and Fungal Strain

All the chemicals used were of analytical grade (AR) and purchased from either Qualigens Fine Chemicals, India, or Hi-Media Laboratories, India or Ranbaxy Fine Chemicals Limited, India.A laboratory Cr(VI) tolerant fungal strain designated as FCR16 was used for present studies. FCR16 was grown and maintained on Potato Dextrose liquid/solidified medium as per the requirement.FCR16 was identified by 18 s rDNA sequencing. The analysis of the nucleotide sequencing was carried out using Blast-n tool at NCBI (http://blast.ncbi.nlm.nih.gov/Blast.cgi). The phylogenetic tree was constructed by neighbour joining method using MEGA version 4.0 [17].


## 2.2. Preparation of Fungal Biomass for Cr(VI) Ion Biosorption

FCR16 was inoculated by transferring a block of fungal growth (16 mm diameter) on Potato Dextrose agar plates (grown for three days at 30°C) using sterile cup borer to 500 mL Erlenmeyer flasks filled with 200 mL of culture medium composed of the following (g/L): Potatoes infusion forms, 200; and Dextrose, 20 and incubated on to a rotary shaker at 150 rpm for five days at 30°C. Upon incubation, the biomass produced was separated by filtration and the resulting biomass was washed thoroughly for several times with distilled water. The biomass was treated with hydrochloric acid (6N), washed with distilled water to bring the pH of the biomass in neutral range, and then was used directly for Cr(VI) adsorption studies from electroplating industrial wastewater, considering the higher Cr(VI) biosorption capacity of acid-treated biomass of FCR16 in pure Cr(VI) solution.


## 2.3. Characteristics of Effluent Sample

Electroplating effluent was collected from an electroplating unit located in Industrial Estate of Vadodara, Makarpura, Gujarat, India. The characteristics of electroplating effluent are listed in Table2. The major contaminants of wastewater were Cr(VI), Ni, and Fe. In addition, pH of the waste water was highly acidic that is, 1.5.Table 2
Physical and chemical characteristics waste water collected from effluent of electroplating industry.
Parametersmg/LCOD32Ammonium nitrate61.6Total solids10.30Total dissolved salts10.1Chlorides350SulphateNDSulphidesNDNickel32.8Iron10.31Oil and grease10.66Hexavalent Cr(VI)5,000pH1.5ColorYellow to brown


## 2.4. Batch Experiment

The biomass (at biomass dose of 10 mg/mL) of FCR16 was mixed with 100 mL of diluted effluent containing Cr(VI) in the range from 100 to 500 mg/L. Apart from Cr(VI) concentration adjustments, no other pretreatment was given to the effluent. After mixing, the experimental set was kept on shaker (150 rpm) at 30°C. 1 mL sample was withdrawn at regular time interval and residual Cr(VI) was measured.


## 2.5. Kinetics of Cr(VI) Biosorption

Pseudo-first-order and pseudo-second-order rate equations have been used for modelling the kinetics of Cr(VI) ion biosorption [26]. Linear form of pseudo-first-order rate equation is expressed as follows:(1)log⁡(qeq-qt)=log⁡qeq-k1t2.303,
where qt and qeq are sorption capacity at time t and at equilibrium, respectively, and k1 is pseudo-first-order rate constant.In case the biosorption follows pseudo-first-order rate equation, a plot oflog(qeq-qt) versus t should generate straight line with intercept of logqeq and slope of -k1/2.303.Similarly, linear form of pseudo-second-order rate equation is expressed as(2)tqt=1k2(qeq)2+tqeq,
where k2 is pseudo-second-order rate constant.In case the biosorption follows pseudo-second-order rate equation, a plot oft/qt versus t should generate a straight line with intercept of 1/k2qeq2 and slope of 1/qeq.The shape (linearity) of graph and comparison of experimental and calculatedqeq values can help in deciding which kinetic model is followed by biosorption process. Another important factor which influences the kinetic model is the value of coefficient of determination: R2. A value of R2>0.9 shows the suitability of model for describing the kinetics.


## 2.6. Equilibrium Model for Cr(VI) Biosorption by FCR16 Biomass from Electroplating Wastewater

Biosorption data were analyzed using Langmuir and Freundlich equilibrium isotherms to determine the feasibility of Cr(VI) ion biosorption. The Freundlich isotherm equation is an empirical equation based on the biosorption on a heterogeneous surface suggesting that the binding sites are not equivalent or dependent [27]. Langmuir isotherm equation is based on monolayer sorption onto a surface with finite number of identical sites, which are homogeneously distributed over the sorbent surface [28].


## 2.7. Analysis of Cr(VI) Ions

The concentration of the Cr(VI) ions was determined spectrophotometrically after complexation of the Cr(VI) with 1, 5-diphenylcarbazide [29]. The absorbance was recorded at 540 nm and concentration was determined from the calibration curve.Characterization of effluent was done according to standard methods described by APHA [30].


## 3. Results and Discussion

The Cr(VI) tolerant fungal strain designated as FCR16 was identified asTrichoderma gamsii with 99% similarity (accession number: JF834064). The phylogenetic relationship of FCR16 with other related fungal species is presented in Figure 1.Figure 1
Phylogenetic affiliation based on 18 s rRNA gene sequence comparison over 561 nucleotides showing the relationship of FCR16 with other fungal strains. The value at node represents percentage of 1000 bootstrap replicates. Number in bracket represents GenBank accession numbers.


### 3.1. Effect of Contact Time on Cr(VI) Ion Biosorption from Electroplating Industrial Effluent by Acid-Treated Biomass ofT. gamsii

Electroplating industrial effluent (pH: 1.5) containing 5000 mg/L of Cr(VI) ions was diluted (without any pretreatment of effluent) 50 times with distilled water to get the final concentration of 100 mg Cr(VI)/L.Figure2 shows the role of contact time on Cr(VI) biosorption using acid-treated biomass of T. gamsii at biomass dose of 10 mg/mL under shaking condition of 150 rpm. It was found that biosorption increased from 50 to 89% as the contact time was increased from 0 to 420 minutes. As illustrated, one gram of T. gamsii biomass could remove 89% of Cr(VI) ions at equilibrium. Metal biosorption is reported to be biphasic process, with rapid sorption of metal ions to the surface groups of the biomass constituting the first phase followed by a second phase during which diffusion of metal to internal binding sites on the biomass limits the sorption rate [31, 32]. Furthermore, the Cr(VI) biosorption depends on protonation and deprotonation of the cell wall polymer functional group relative to their pKa. At low pH, the protonation of functional group gives an overall positive charge to the fungal biomass, thereby leading to enhanced Cr(VI) biosorption. In the present study the acidic nature of the electroplating effluent and acid pretreatment of biomass together led to the significant Cr(VI) biosorption as demonstrated by higher Cr(VI) removal (%) in Figure 2. This biosorption efficiency was slightly lower than Cr(VI) ion removal efficiency of T. gamsii (50.6 mg/g biomass) from pure solution of Cr(VI) (data not shown). This may be attributed to competition between Cr(VI) and other metal ions present in electroplating effluent for the functional groups on the surface of biomass. Similar reduced Cr(VI) biosorption efficiency from electroplating industrial waste by A. niger has been reported by Kumar et al. [33].Figure 2
Time course for Cr(VI) removal by biosorption usingT. gamsii biomass from electroplating industrial waste, diluted to a final Cr(VI) concentration of 100 mg/L.


### 3.2. Effect of Initial Cr(VI) Ion Concentration of Effluent on Biosorption

The biosorption of Cr(VI) ions from electroplating effluent was carried out for 420 minutes at 150 rpm using acid-treated biomass (10 mg/mL) ofT. gamsii with series of dilutions of effluent to get final Cr(VI) concentration in the range of 100 to 500 mg/L. It can be demonstrated from the experimental results that uptake capacity (qeq, mg/g biomass) increased from 7.06 mg to 42.71 mg Cr(VI)/g acid-treated biomass of T. gamsii (Figure 3) when initial Cr(VI) concentration was increased from 100 to 500 mg/L, suggesting the increased propelling force provided by higher initial Cr(VI) ion concentration to overcome all mass transfer resistance of metal ions between the aqueous and solid phases, consequently, resulting in higher probability of collision between Cr(VI) ions and biosorbents [25, 34]. The Cr(VI) biosorption capacity of acid-treated T. gamsii biomass (42.71 mg/g) was comparable or better than other biosorbents reported for removal of Cr(VI) from electroplating effluent, namely, Padina boergesenii(49 mg/g), Lentinus edodes (21.5 mg/g), C. lipolytica (10 mg/L), and A. niger (65% from electroplating effluent contaminated with 47 mg/L Cr(VI)) [34–36].Figure 3
Cr(VI) biosorption (mg/g) byT. gamsii biomass from electroplating industrial waste diluted to final Cr(VI) concentration in the range from 100 to 500 mg/L.Kinetic studies based on pseudo-second-order plot oft/qt versus t (2) indicated that the biosorption of Cr(VI) ion followed pseudo-second-order rate of reaction in the Cr(VI) concentration range of 100 to 500 mg/L (Figure 4). The values of experimental/calculated equilibrium uptake capacities (qeqexp and qeqcal), correlation regression coefficient (R2), and second-order rate constants (k2) are presented in Table 3. The values of equilibrium uptake capacity increased (from 7.26 to 44.8 mg/g biomass) whereas second-order rate constant (k2) was found to decrease (from 0.376 to 0.075) with increasing concentration of Cr(VI) ions (from 100 to 500 mg/L). This shows that the chromium sorption kinetics is strongly dependent on mass transfer phenomenon [25]. The rate of biosorption increases at slower rate compared to the increase in concentration due to sorption site saturation, which thus leads to the decrease in rate constant. The calculated uptake capacity values estimated from second-order kinetic model were in agreement to the experimental values. Additionally, correlation regression coefficients of pseudo-second-order model are quite high (R2>0.98), very close to unity. Therefore, Cr(VI) ion biosorption by acid-treated biomass followed pseudo-second-order model. These observations are in agreement with the observations made by Ye et al. [37] where they have used Candida lipolyticaand dewatered sewage sludge for biosorption of Cr(VI) ions from electroplating wastewater.Table 3
Second-order kinetic parameters for biosorption of Cr(VI) byT. gamsiibiomass at various dilutions of electroplating industrial wastewater.
Cr(VI), mg/Lqeqexp, mg/g (experimental)qeqcal, mg/g (calculated)k2R21007.0647.260.3760.99215012.0912.280.2180.99140037.8539.060.0540.98850042.7144.80.0750.995Figure 4
Linearized second-order kinetic plot of Cr(VI) biosorption byT. gamsii biomass at varying initial concentrations of Cr(VI).


### 3.3. Adsorption Isotherms for Cr(VI) Ion Biosorption

The experimental values of equilibrium uptake capacities of Cr(VI) ions from electroplating effluent (Table3) by acid-treated biomass of T. gamsii were analyzed by Freundlich and Langmuir isotherm models. Langmuir and Freundlich isotherms are single-solute adsorption isotherm models, which are widely used to analyze data for effluent treatment application to characterize the interaction of metal ions with biomass preparations [13]. The linearized plots of Freundlich and Langmuir isotherm model for biosorption of Cr(VI) ions from electroplating effluent by acid-treated biomass of T. gamsii are presented in Figure 5. It can be seen that R2 value for the Freundlich isotherm is 0.9423 against the Langmuir isotherm R2 value of 0.5046. Analysis of correlation regression coefficient shows that biosorption process fits better into Freundlich isotherm (Figure 5). The Langmuir and Freundlich adsorption constants calculated from the corresponding isotherms are presented in Table 4. The Freundlich isotherm constants kf and n were calculated as 8.3 and 1.13, respectively. The high magnitude of kf and n illustrates high adsorption capacity of biomass.Table 4
Isotherm parameters for Cr(VI) biosorption byT. gamsii biomass at various dilutions of electroplating industrial wastewater.
Freundlich isotherm constantsLangmuir isotherm constantnKf, mg/gR2bQ, mg/gR21.138.30.94230.068133.330.5046Biosorption isotherm: (a) Freundlich and (b) Langmuir isotherm for Cr(VI) biosorption byT. gamsii biomass at various dilutions of electroplating industrial waste water.
(a)(b)All these results showed that Freundlich isotherm model fitted the results quite well which are in agreement with the heterogeneity of sorbent (T. gamsii biomass) surface. Binding sites are not independent and adsorption energy of a metal binding site depends on whether or not the adjacent sites are already occupied. Thus, the adsorption of Cr(VI) ions by T. gamsii seems to be a complex process involving multilayer, interactive, or multiple-site type binding.


## 3.1. Effect of Contact Time on Cr(VI) Ion Biosorption from Electroplating Industrial Effluent by Acid-Treated Biomass ofT. gamsii

Electroplating industrial effluent (pH: 1.5) containing 5000 mg/L of Cr(VI) ions was diluted (without any pretreatment of effluent) 50 times with distilled water to get the final concentration of 100 mg Cr(VI)/L.Figure2 shows the role of contact time on Cr(VI) biosorption using acid-treated biomass of T. gamsii at biomass dose of 10 mg/mL under shaking condition of 150 rpm. It was found that biosorption increased from 50 to 89% as the contact time was increased from 0 to 420 minutes. As illustrated, one gram of T. gamsii biomass could remove 89% of Cr(VI) ions at equilibrium. Metal biosorption is reported to be biphasic process, with rapid sorption of metal ions to the surface groups of the biomass constituting the first phase followed by a second phase during which diffusion of metal to internal binding sites on the biomass limits the sorption rate [31, 32]. Furthermore, the Cr(VI) biosorption depends on protonation and deprotonation of the cell wall polymer functional group relative to their pKa. At low pH, the protonation of functional group gives an overall positive charge to the fungal biomass, thereby leading to enhanced Cr(VI) biosorption. In the present study the acidic nature of the electroplating effluent and acid pretreatment of biomass together led to the significant Cr(VI) biosorption as demonstrated by higher Cr(VI) removal (%) in Figure 2. This biosorption efficiency was slightly lower than Cr(VI) ion removal efficiency of T. gamsii (50.6 mg/g biomass) from pure solution of Cr(VI) (data not shown). This may be attributed to competition between Cr(VI) and other metal ions present in electroplating effluent for the functional groups on the surface of biomass. Similar reduced Cr(VI) biosorption efficiency from electroplating industrial waste by A. niger has been reported by Kumar et al. [33].Figure 2
Time course for Cr(VI) removal by biosorption usingT. gamsii biomass from electroplating industrial waste, diluted to a final Cr(VI) concentration of 100 mg/L.


## 3.2. Effect of Initial Cr(VI) Ion Concentration of Effluent on Biosorption

The biosorption of Cr(VI) ions from electroplating effluent was carried out for 420 minutes at 150 rpm using acid-treated biomass (10 mg/mL) ofT. gamsii with series of dilutions of effluent to get final Cr(VI) concentration in the range of 100 to 500 mg/L. It can be demonstrated from the experimental results that uptake capacity (qeq, mg/g biomass) increased from 7.06 mg to 42.71 mg Cr(VI)/g acid-treated biomass of T. gamsii (Figure 3) when initial Cr(VI) concentration was increased from 100 to 500 mg/L, suggesting the increased propelling force provided by higher initial Cr(VI) ion concentration to overcome all mass transfer resistance of metal ions between the aqueous and solid phases, consequently, resulting in higher probability of collision between Cr(VI) ions and biosorbents [25, 34]. The Cr(VI) biosorption capacity of acid-treated T. gamsii biomass (42.71 mg/g) was comparable or better than other biosorbents reported for removal of Cr(VI) from electroplating effluent, namely, Padina boergesenii(49 mg/g), Lentinus edodes (21.5 mg/g), C. lipolytica (10 mg/L), and A. niger (65% from electroplating effluent contaminated with 47 mg/L Cr(VI)) [34–36].Figure 3
Cr(VI) biosorption (mg/g) byT. gamsii biomass from electroplating industrial waste diluted to final Cr(VI) concentration in the range from 100 to 500 mg/L.Kinetic studies based on pseudo-second-order plot oft/qt versus t (2) indicated that the biosorption of Cr(VI) ion followed pseudo-second-order rate of reaction in the Cr(VI) concentration range of 100 to 500 mg/L (Figure 4). The values of experimental/calculated equilibrium uptake capacities (qeqexp and qeqcal), correlation regression coefficient (R2), and second-order rate constants (k2) are presented in Table 3. The values of equilibrium uptake capacity increased (from 7.26 to 44.8 mg/g biomass) whereas second-order rate constant (k2) was found to decrease (from 0.376 to 0.075) with increasing concentration of Cr(VI) ions (from 100 to 500 mg/L). This shows that the chromium sorption kinetics is strongly dependent on mass transfer phenomenon [25]. The rate of biosorption increases at slower rate compared to the increase in concentration due to sorption site saturation, which thus leads to the decrease in rate constant. The calculated uptake capacity values estimated from second-order kinetic model were in agreement to the experimental values. Additionally, correlation regression coefficients of pseudo-second-order model are quite high (R2>0.98), very close to unity. Therefore, Cr(VI) ion biosorption by acid-treated biomass followed pseudo-second-order model. These observations are in agreement with the observations made by Ye et al. [37] where they have used Candida lipolyticaand dewatered sewage sludge for biosorption of Cr(VI) ions from electroplating wastewater.Table 3
Second-order kinetic parameters for biosorption of Cr(VI) byT. gamsiibiomass at various dilutions of electroplating industrial wastewater.
Cr(VI), mg/Lqeqexp, mg/g (experimental)qeqcal, mg/g (calculated)k2R21007.0647.260.3760.99215012.0912.280.2180.99140037.8539.060.0540.98850042.7144.80.0750.995Figure 4
Linearized second-order kinetic plot of Cr(VI) biosorption byT. gamsii biomass at varying initial concentrations of Cr(VI).


## 3.3. Adsorption Isotherms for Cr(VI) Ion Biosorption

The experimental values of equilibrium uptake capacities of Cr(VI) ions from electroplating effluent (Table3) by acid-treated biomass of T. gamsii were analyzed by Freundlich and Langmuir isotherm models. Langmuir and Freundlich isotherms are single-solute adsorption isotherm models, which are widely used to analyze data for effluent treatment application to characterize the interaction of metal ions with biomass preparations [13]. The linearized plots of Freundlich and Langmuir isotherm model for biosorption of Cr(VI) ions from electroplating effluent by acid-treated biomass of T. gamsii are presented in Figure 5. It can be seen that R2 value for the Freundlich isotherm is 0.9423 against the Langmuir isotherm R2 value of 0.5046. Analysis of correlation regression coefficient shows that biosorption process fits better into Freundlich isotherm (Figure 5). The Langmuir and Freundlich adsorption constants calculated from the corresponding isotherms are presented in Table 4. The Freundlich isotherm constants kf and n were calculated as 8.3 and 1.13, respectively. The high magnitude of kf and n illustrates high adsorption capacity of biomass.Table 4
Isotherm parameters for Cr(VI) biosorption byT. gamsii biomass at various dilutions of electroplating industrial wastewater.
Freundlich isotherm constantsLangmuir isotherm constantnKf, mg/gR2bQ, mg/gR21.138.30.94230.068133.330.5046Biosorption isotherm: (a) Freundlich and (b) Langmuir isotherm for Cr(VI) biosorption byT. gamsii biomass at various dilutions of electroplating industrial waste water.
(a)(b)All these results showed that Freundlich isotherm model fitted the results quite well which are in agreement with the heterogeneity of sorbent (T. gamsii biomass) surface. Binding sites are not independent and adsorption energy of a metal binding site depends on whether or not the adjacent sites are already occupied. Thus, the adsorption of Cr(VI) ions by T. gamsii seems to be a complex process involving multilayer, interactive, or multiple-site type binding.


## 4. Conclusion

In conclusion, the present study provides the practical application of theT. gamsii biomass. Acid-treated biomass of T. gamsiiis effective in removing Cr(VI) ions from acidic (pH 1.5) electroplating effluent contaminated with 5000 mg/L of Cr(VI) and other coexisting metal ions. At initial pH of electroplating effluent and biomass dose of 10 mg/mL, 89% of Cr(VI) ions were removed within 420 minutes of contact time. The biosorption of Cr(VI) ions increased with increasing contact time and initial Cr(VI) ion concentration. Kinetic model developed based on the values of equilibrium uptake capacity, correlation regression coefficient, and rate constants illustrated that the biosorption follows second-order rate of reaction. The Freundlich adsorption model was found to better describe the phenomenon of Cr(VI) biosorption onto acid-treated biomass of T. gamsii. Thus, the results suggest the reasonable potential of acid-treated biomass of T. gamsii as sorbent for removal of Cr(VI) from electroplating effluents.



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