Paspalum notatum Grass-waste-based Adsorbent for Rhodamine B Removal from Polluted Water

The potential of Paspalum notatum grass waste to adsorb Rhodamine B dye from aqueous phase is reported in this research. The grass waste was activated and characterized through various techniques to analyze the chemical (FTIR), morphological (SEMEDX), and thermal (TGA) changes incorporated through the activation process. The pollutant removal efficiency of the raw and modified adsorbents was studied by varying different process parameters in a batch process. The maximum capacity of adsorption which was observed for grass waste and activated grass waste was 54 mg g–1 and 72.4 mg g–1 respectively. Among the various kinetic models, the pseudo-second order model gives the best regression results. However, the intraparticle diffusion-adsorption model showed that the diffusion within pores controlled the adsorption rate. Thermodynamic analysis of this process revealed that Rhodamine B adsorption was endothermic and spontaneous in nature. The results of this study show that grass waste has the potential to be used as an adsorbent for the treatment of colored water.


Introduction
Organic dyes are used in various industries such as polymer, printing, paper and pulp, textile, and cosmetics to increase the aesthetics of their final products. Most of these dyes are hazardous due to their acute and chronic health effects, some being classified as carcinogenic. Therefore, the discharge of dyes into an aqueous environment poses a serious threat to human as well as aquatic life 1 . Among the toxic organic dyes, Rhodamine B is widely utilized in textile dying and in laboratories as a biological stain. Rhodamine B has been banned in food processing applications because of its carcinogenic nature. Therefore, it is imperative to either remove or minimize its concentration in wastewater to a safer limit before discharging into aquatic streams 2,3 . Various treatment methods, such as Fenton oxidation, photocatalytic oxidation, adsorption, coagulation, and membrane separation have been used to treat dye-containing wastewater [4][5][6][7] . Adsorption is one of the most economical, feasible, and cost-effective technologies. Activated carbon is used extensively as a conventional adsorbent due to its enhanced surface reactivity, high surface area, and high adsorp-tion capacity. However, commercial activated carbon is quite expensive. Moreover, the reusability of activated carbon is still a challenge due to the loss of 10-15 % activated carbon during the regeneration process, which increases the overall treatment cost 8 . Therefore, adsorption of dyes using cheaper materials, such as agricultural wastes, has gained great attention. It has been estimated that about 1000/million tons of agricultural waste are being produced annually worldwide, but due to lack of resources, this waste cannot be utilized to its full potential. However, agricultural waste has received wide interest nowadays in the field of wastewater treatment due to its abundant availability, low cost, and ease of modification [9][10][11] .
Various agro-based adsorbents have been researched for the treatment of dye-bearing effluents. Some of the agricultural wastes used as adsorbents include date palm fibers 12 , banana fibers 13 , straw 14 , sugar cane bagasse 15 , Artocarpus odoratissimus stem axis 16 , water lettuce 17 , Artocarpus altilis (breadfruit) 18 , durian seed 19 , orange peel 20 , wheat husk 21 . Ramaraju studied the performance of nitric acid-modified and peroxide-modified rice husks for malachite green removal from aqueous solution. They reported that the adsorption capacity of perox-ide-modified rice husk (26.6 mg g -1 ) was superior to that of nitric acid-modified rice husk 11 . Hameed studied the potential of grass for the removal of methylene blue and reported an excellent adsorption capacity of 458 mg g - 1 9 . Kumar and Porkodi investigated the adsorption of methylene blue in Paspalum notatum by studying mass transfer and adsorption kinetics. They reported that the adsorption potential of Paspalum notatum was observed to be 31 mg g - 1 22 . The adsorption capacity of grass can be enhanced by modifying its physical/chemical structure. Chen et al. stated that the acid treatment of lawn grass increased its removal efficiency threefold for methylene blue adsorption 23 . The enhancement in the adsorption capacity was attributed to the increased surface functional groups induced by the chemical treatment. Cellulose, hemicellulose, lignin, and limonene are the main constituents of any grass, which provide additional functional groups, i.e., carboxyl, hydroxyl, and phenol. These functional groups can also be modified by different surface treatments of the grass to increase its affinity towards pollutants 24 . Kumar et al. removed lignin from the core of Vetiveria zizanioides grass and reported higher adsorption of chromium due to an increase in the surface area 25 . Different types of modified grass were already tested for the removal of many pollutants. However, there is a lack of studies for the use of acid-treated Paspalum notatum grass for Rhodamine B removal.
The aim of the current research work was to compare the adsorption capacity of Paspalum notatum, chlorophyll, and limonene-removed Paspalum notatum for Rhodamine B removal. The experiments were conducted through the batch adsorption process, and the effects of different process parameters were investigated. The synthesized adsorbent was analyzed for spectroscopic and surface properties by Fourier Transform Infrared Spectroscopy (FTIR) and Scanning Electron Microscopy (SEM), respectively. The experimental results were also analyzed thermodynamically and kinetically to study the spontaneity and adsorption mechanism.

Preparation of adsorbent
The GW was firstly cleaned with demineralized water to wash the mud and dirt from its surface. The washed sample was dried at 60 °C in an oven for 24 h. The low temperature was selected to avoid thermal deactivation of the surface of the grass. The dried GW was ground and sieved to obtain a uniform particle size. Fifty grams of ground GW powder was soaked in a beaker containing 500 mL of 1 M isopropanol solution. The GW powder was left to soak for 24 hours to remove organic constituents such as chlorophyll and limonene. After filtration, the mixture residue was cleaned with double demineralized water until a colorless filtrate was observed. The residue was then dried at 60 °C in an oven for 24 h. The chlorophyll-removed GW powder was then subjected to acid activation. Twenty grams of chlorophyll-removed GW powder was boiled in 500 mL of 0.75 M HCl solution under total reflux conditions for 4 hours. The solid was then filtered and the residue rinsed several times with demineralized water to remove the acid contents. The solid residue was then dried at 80 °C in an oven for 24 h. The dried acid-treated GW was sealed in an airtight jar for further use. The acid-activated GW is further herein abbreviated as "AGW".

Material characterization
The IR spectra of raw and activated GW were recorded on the FTIR spectrometer (Perkin Elmer, Spectrum two, USA) using ZnSe-ATR (Attenuated total reflectance) module. A half-gram of the sample was kept in a desiccator before the analysis in order to remove the adsorbent moisture. The thermal stability of the adsorbent was analyzed by a thermogravimetric analyzer (TA instrument, SDT-Q600, UK Ltd.). The analysis was performed in a nitrogen environment over the temperature range 30-900 °C at 10 °C min -1 . The surface morphological property was observed on Field Emission Scanning Electron Microscope (MIRA3, TES-CAN, Cambridgeshire, UK) at 20 kV accelerating voltage. BET (Brunauer-Emmett-Teller) surface area of raw and modified grass was determined using the Micromeritics ASAP2020 analyzer.

Adsorption experiments
The adsorption of Rhodamine B dye was tested through the batch adsorption process. Accurately weighted Rhodamine B was dissolved in 1 L demineralized water to prepare a 100 ppm stock solution of dye. The required volume of stock solution was further diluted to obtain 100 mL of working solution of desired Rhodamine B concentration in an Erlenmeyer flask. The working solution pH was maintained by 0.1 M solutions of NaOH and HCl. Initially, 0.3 g adsorbent dose was taken into solution and put on a multi-point orbital shaker at 150 rpm for 6 hours. The solution was filtered, and the filtrate analyzed using UV-Vis-NIR double beam spectrophotometer (Perkin Elmer Lambda 950, UK) at λ max = 550 nm to determine the removal efficiency. No sorption was observed either on the filter paper or on the glassware. The effects of adsorbent dosage (0.05 -4 g), time (1 -390 min), initial concentration (10 to 500 ppm), pH (2)(3)(4)(5)(6)(7)(8)(9)(10), and temperature (20 to 50 °C) on the adsorption process were studied. The quantity of the adsorbed dye was calculated using Equations 1 and 2.
where, q e (mg g -1 ) is the equilibrium uptake capacity, V is the solution volume (L), γ i (mg L -1 ) is the initial Rhodamine B concentration in solution, γ fe (mg L -1 ) is the final Rhodamine B concentration in solution at equilibrium, and w is the adsorbent weight (g).

Adsorption kinetics
Various proposed kinetic models provide useful data of adsorption mechanism in order to enhance the adsorption capability and scale-up the feasibility of the adsorption process. Among these models, pseudo-first order describes the rate of adsorption uptake as a linear function of the gradient of adsorption. The linear formation of pseudo-first order kinetic model can be presented by Eq. 3.

( )
where, K 1 (min -1 ) is pseudo-first order constant, q e (mg g -1 ) and q t (mg g -1 ) are the equilibrium and instantaneous adsorption uptake of Rhodamine B over sorbent surface, respectively. The intercept and the slope of "t" vs log (q e -q t ) plot may determine the parameter of the pseudo-first order model. The pseudo-second order model is given as Eq. 4.
where, k 2 (g mg g -1 ) is pseudo-second order kinetic rate constant. Intercept and slope of the plot of t vs e t q may be used to estimate the parameters of pseudo-second order model, i.e., k 2 and q e . The Elovich kinetic model, in its empirical form, has been used extensively to explain the chemisorption and surface heterogeneity of the adsorbent 26 . The linear formation of the Elovich kinetic model is given as Eq. 5.
where, α is a constant associated with the rate of chemisorption, and β is related to the surface coverage of sorbent by the Rhodamine B. The plot of q t vs ln(t) is usually used to determine the α and β parameters. The intraparticle diffusion model was employed in order to investigate the mechanism of diffusion of adsorbate, i.e., film diffusion, surface diffusion, or pore diffusion. The mathematical relation of the intraparticle diffusion model proposed by Weber and Morris is given by Equation 6.
where, k i (mg g -1 min 1 2 − )is a constant of this model, and α (mg g -1 ) corresponds to the boundary layer thickness at the interface of solid-liquid. The boundary layer influence will increase at its higher value, while intraparticle diffusion will be taken as only rate-limiting step if "α" is zero.
To investigate the pore diffusion step in the adsorption of Rhodamine B by GW and AGW, the Bangham model was used. If intraparticle diffusion is the only rate-limiting step in the adsorption, then the Bangham model plot should be a straight line (linear). However, non-linearity along with intercept depicted both the film diffusion as well as pore diffusion as the rate-limiting steps in the adsorption process. The linear form of the Bangham model can be written as Eq. 7 27 .
where, γ i (mg L -1 ) is the initial concentration of Rhodamine B, w (g) is the weight per liter of the adsorbent, and K b and β are the constants of the Bangham model, and that can be estimated by the intercept and slope, respectively.

Adsorption isotherms
The distribution of pollutant over the solid surface can be explained by various models of equilibrium adsorption isotherm, i.e., Langmuir, Freundlich, and Redlich-Peterson (RP) isotherm models 28,29 . Moreover, isotherm analysis can also be used to determine the maximum uptake potential of an adsorbent for the scale-up of the adsorption process. Two-and three-parameter models were employed in this study.
Langmuir isotherm (two-parameter model) assumes constant enthalpy and activation energy of each active site on the sorbent surface. Furthermore, the Langmuir isotherm model assumes that no hindrance is caused by the nearby active site, and thus, reveals monolayer adsorption of dye molecules on the adsorbent homogeneous surface 30 . The mathematical expression of this model is represented as where, q m (mg L -1 ) is the maximum uptake adsorption capacity, and K L (L mg -1 ) is the constant of the Langmuir model associated with the free energy of the adsorption process. Freundlich isotherm (two-parameter model) pre supposes that the adsorption activation energy varies for each active site. Therefore, it depicts the multilayer adsorption of pollutant on the adsorbent surface due to heterogeneity 31 . The non-linear expression for the Freundlich isotherm model can be expressed as Eq. 9.
where, K F (mg g -1 ) is a constant associated with relative uptake capacity of adsorbent, and n gives the heterogeneity of the surface. Redlich-Peterson is a three-parameter isotherm model that includes the characteristics of both Langmuir and Freundlich models, and is therefore used as a compromise between the two isotherm models. The ratio of K R /α R depicts the maximum adsorption capacity of the adsorbent. The non-linear mathematical statement for Redlich-Peterson isotherm is given in Eq. 10 32 .
where n is the number of data points, and p is the total number of parameters in the model under consideration.

Adsorption thermodynamics
Thermodynamic variables, i.e., Gibb's free energy, enthalpy, and entropy are imperative to assess the practicality and nature of the adsorption process. Eqs. 14 -16 were used for the thermodynamic analysis of the adsorption process.
where, K is the dimensionless distribution coefficient for the adsorption process, γ A is Rhodamine B concentration on the adsorbent surface, γ S is filtrate concentration of Rhodamine B, T (K) is the absolute temperature, Ristheuniversalgasconstant,ΔG (kJ mol -1 ) isthechangeinGibb'senergy,∆S (kJ mol -1 ) is the changeinentropy,and∆H (kJ mol -1 ) is the enthalpy change during the adsorption process.

Results and discussion
FTIR study GW and AGW infrared spectra are shown in Fig. 1. For GW, the two acuminated peaks at wavenumbers 3848 cm -1 and 3744 cm -1 belong to the isolated OH functional groups in the organo-silicon compounds of the grass biomass. A broad and sharp peak centered at 3362 cm -1 may be attributed to stretching vibrations of hydrogen-bonded hydroxyl functional group that is associated with either polysaccharides or silanol compounds. The two consecutive peaks at 2922 cm -1 and 2848 cm -1 are ascribed to symmetric and asymmetric extension and contraction of C-H in the saturated hydrocarbons/carbohydrates containing methyl and methylene functional groups. The sturdy peak at 2358 cm -1 shows the occupancy of adsorbed CO 2 from the environment 34 . The transmittance peaks at 1689 and 1649 cm -1 may be linked to the stretching vibrations of C=C present in unconjugated cis-alkenes. The peak at 1741 cm -1 corresponds to the stretching vibrations of -C=O in the GW. Moreover, the small peak at 1531 cm -1 is probably because of the interaction of C-N stretching and N-H bending. The transmit-tance peaks at 1390 cm -1 emanate from the in-phase and out-of-phase bending vibrations of two -CH 3 functional groups attached to a common carbon in the grass. The broad peak that has a minimum at 1039 cm -1 is associated with C-O stretching vibrations, asymmetric stretching mode of Si-O-Si, strong stretching vibrations of Si-O and C-H outof-plane bending. The activation of GW imparted significant changes in the grass structure, as shown in Fig. 1 for AGW. The absence of peaks at higher wavenumbers (i.e., 3848 cm -1 and 3744 cm -1 ) may have been due to the dissolution of limonene as a result of the alcoholic pretreatment and acid leaching of the grass 35 . Furthermore, the peak at 1531 cm -1 vanished, which reflects the removal of the amide II present in chlorophyll. The exclusion of these peaks in AGW confirms the successful removal of chlorophyll and limonene from the raw grass 23,36 . The activation processes increase the aromaticity in AGW by removing silica and other compounds, resulting in the presence of a sharp transmittance peak at 874 cm -1 .

Thermogravimetric analysis
The thermograms of both GW and AGW are summarized in Fig. 2. The mass loss pattern of GW exhibits two major phases, while the degradation of AGW displays four distinct phases in the examined temperature range. The first phase (caped between 33 °C to 148 °C) is the same for both GW and AGW, and approximately 10 % of total mass loss occurred in this range. This mass loss may be associated with the release of the water molecules and light volatiles retained on the adsorbent surface. The thermal decomposition of GW in the range of 290 °C -600 °C gives a major loss in weight as represented by a broader peak in the derivative weight loss curve. This corresponds to the volatilization of the oxygenated compounds, i.e., cellulose, hemicellulose, and lignin in the GW 37,38 . For AGW, the thermal degradation starts a little earlier at around 167 °C and ends at 575 °C, after which the mass loss becomes constant. This decrease in the initial degradation temperature in AGW is due to the removal of chlorophyll from the grass, which binds the lignin chains through hydrogen bonding. The removal of chlorophyll induced thermal instability in the grass. Moreover, the acid activation reduces the polysaccharides and carbohydrates in GW, which decreases its resistance towards thermal degradation 39,40 . The broad tailing peak in AGW represents the char oxidation, which was not observable in GW due to the overlapping of decomposition temperatures of the oxygenated compounds. Raw GW may have a more complex structure because of overlapping saccharide compounds as compared to AGW. In addition, the activation process induced a structural and compositional change, which produced distinct sharp peaks in AGW, as may be observed in Fig. 2. Moreover, the percentage of the residual weight of GW was higher (i.e., 16 %) as compared to AGW, due to the higher content of impurities in GW.

SEM/EDX and porosity analysis
The surface morphologies of GW and AGW are presented in Fig. 3. Prominent textural changes are observable on the grass surface before and after activation. The surface of GW appears to be rough, uneven, defibrillated, and replete with surface impurities (Fig. 3a). Whereas, the activation process abraded the surface of the grass and created non-uniform/irregular cavities at the surface, as may be seen in Fig. 3b. Apparently, there is no major change

F i g . 2 -Thermogravimetric analysis of GW and AGW
in the framework of the grass, which indicates that the grass has good mechanical properties. The porosity analysis revealed that the BET surface area of GW was 0.0068 m 2 g -1 , and after acid activation, the surface area of AGW was 0.35 m 2 g -1 . An increase in surface area is in agreement with SEM images in Fig. 3. The variations in the composition of elements were determined by spot analysis using EDX spectroscopy, and results are reported in Table  1. Ca and Fe were completely removed from AGW, because the acid activation leached all inorganic mineral impurities. However, a relative increase in silica weight percentage was observed, which showed its inherent characteristic of being insoluble in acid.

Analysis of adsorption process parameters
The viability of the adsorption process strongly depends on the amount of adsorbent required to abate the pollutant from the aqueous phase. The adsorbent dosage effect on the uptake of Rhodamine B is presented in Table 2. The higher percentage removal of pollutant may be observed by increasing dosage of the adsorbent for both AGW and GW. This is probably because of the availability of a greater number of active sites for Rhodamine B. However, no significant increase in percentage re-moval of Rhodamine B was observed as the dosage of adsorbent increased, probably because of the attainment of equilibrium. This shows that the availability of more adsorbent sites, in terms of adsorbent dosage, would not guarantee the capture of more pollutants under given experimental conditions. Moreover, the percent adsorption of AGW is higher than that of GW due to the removal of limonene and chlorophyll (as was confirmed by the FTIR), which causes a change in physical structure by the formation of irregular cavities on the grass surface after the acidic treatment of grass, and provides more active sites to the Rhodamine B dye, which could be attractive for the adsorption of basic Rhodamine B dye. An amount of 0.3 g of adsorbent was selected for further batch studies. The solution pH is a key parameter while studying the adsorption potential of an adsorbent. Table 2 shows the influence of pH on the adsorption behavior of GW and AGW. As may be observed from Table 2, the adsorption of Rhodamine B decreased as solution pH decreased, and the maximum adsorption capacity was observed at pH 10. This decrease in uptake capacity was ascribed to the force of repulsion between H + ions and the cationic species of the Rhodamine B 41 . The maximum percent removal was observed to be 74.1 and 85.7 for GW and AGW, respectively.

Dynamic analysis
The results of the adsorption of Rhodamine B against time are presented in Table 3. It may clearly be observed that the equilibrium for GW was established earlier than AGW. The GW took around 100 min, while the adsorption onto AGW reached equilibrium after 200 min, as shown in Table 3. A relatively longer time was required for AGW to reach equilibrium, which may be associated with the diffusion of pollutant dye into the cavities present on the surface. Origin (Version 9.1) software was used for the analysis of adsorption dynamics by linear regression of different kinetic models. Table 4 presents a summary of the parametric values of each kinetic model, i.e., pseudo-first and second order intraparticle diffusion, and the Elovich kinetic model. Comparison of the regression coefficient of both models suggested that the regression coefficient (R 2 ) of the pseudo-first order model was relatively low, i.e., R 2 ≤0.95forbothGWandAGW.However, the adsorption of Rhodamine B on both GW and AGW obeyed the pseudo-second order model as R 2 = 0.99 and calculated q e were much closer to the experimental value. The finest organization of experimental data with a pseudo-second order kinetic model may also be confirmed by the least value of chi-square error, i.e., 0.59 and 0.64 for GW and AGW, respectively. The agreement of pseudo-second order kinetic model with experimental data reflects that the adsorption of Rhodamine B onto GW and AGW is a concentration-dependent process.
Pseudo-second order model cannot highlight the rate-limiting step, which could be either film or pore diffusion within the pores of the solid sorbent. The graphical plot of the intraparticle diffusion model, as shown in Fig. 4, is not linear for the observed time range. It may be seen from Fig. 4 that the plot possesses multi-linear portions, which indicates that more than two steps take part in the adsorption of Rhodamine B. Intraparticle diffusion model rate constant, K i1 , has a higher value for AGW than GW, which represents a faster uptake rate at the initial stage. However, the subsequent rate constants, i.e., K i2 and K i3 become smaller, probably due to diffusion in the cavities on the surface of AGW. The values of α indicate the boundary layer thickness, which is significantly higher in the second phase of the intraparticle diffusion. These higher values in both GW and AGW suggest that surface diffusion plays a major role in the overall adsorption process as a rate-determining step. The dynamic data was further analyzed with Elovich kinetic model. The R 2 value of the Elovich model in Table 4 for both GW and AGW indicated that the surface of adsorbents is heterogamous. However, associated values of chi-square error were higher for GW and AGW in the Elovich model. The regression coefficient (R 2 = 0.99) of the Bangham model for both GW and AGW implied that the boundary layer was not the only rate-limiting step, and that pore diffusion also occurs during the adsorption of Rhodamine B.
Isotherm analysis Fig. 5 shows the equilibrium adsorption isotherm of Rhodamine B onto the investigated GW and AGW. Since the data resembled type I isotherm, three phenomenological isotherm models could be used, namely: Langmuir, Freundlich, and Redlich-Peterson (RP) models. The major difference among these models lies in the way that the heat of adsorption varies with surface coverage. Langmuir supposes constant heat of adsorption because of homogeneous surface, Freundlich assumes a heterogeneous adsorbent surface, and RP isotherm model is the combination of the former two models. The non-linear regression of the experimental adsorption isotherm data for both GW and AGW was performed with Origin 9.1 software, and the results are presented in Fig. 5. The values of the pertinent variables are listed in Table 5.
Freundlich isotherm model exhibited a good fit to the experimental isotherm data at low concentration. However, as the concentration of Rhodamine B increased, the modeled curve tended to deviate from the experimental points, as may be seen in Fig. 5. As a result, poor regression coefficients for GW (R 2 = 0.94) and AGW (R 2 = 0.95) were obtained as listed in Table 3. The value of the regression coefficient (R 2 ) for the Langmuir model was closer to unity in comparison to the Freundlich isotherm model, and predicted q e values were better correlated with experimental uptake. Comparison of the goodness of fit of the three-parameter model (i.e., RP isotherm model) with Langmuir showed no improvement in R 2 . However, for GW, the q e of the Langmuir isotherm model showed a relatively smaller value of error function compared to the q e in the RP isotherm model, and therefore, the adsorption of Rhodamine B on GW may be considered as monolayer adsorption. On the other hand, the smallest value of the error function of q e associated with AGW in the RP isotherm model revealed that the data of the experimental isotherm were well fitted by the three-parameter model rather than the two-parameter models, as summarized in Table 5.
Based on the isotherm analysis of AGW, it can be concluded that, at low concentration values, the adsorption of Rhodamine B is monolayer adsorption as the value of the expression R e β α γ is less than 1, and for the higher concentrations, the value of this expression becomes greater than 1, which exhibits the heterogeneous adsorption of Rhodamine B on the adsorbent.

Thermodynamic analysis
The thermodynamic parameters were estimated from the plot of ln(K) vs 1/T (Fig. 6). It is evident from the graphical plot that the adsorption capacity of both GW and AGW increases with the rise in temperature. Table 6 summarizes the values calculated for Gibbs free energy (∆G), change in entropy (∆S), and change in enthalpy (∆H°). The negative num ber of standard Gibbs energy at all examined tem peratures suggested that Rhodamine B adsorption onto both GW and AGW was feasible and spontaneous in nature. The magnitude of Gibbs free energy change was higher for AGW than GW. This could be linked to the removal of chlorophyll and limonene, followed by leaching of metallic impurities that produced more active sites that favored the adsorption of Rhodamine B. The positive value of change in enthalpy showed that the adsorption process was endothermic in nature. Moreover, the enthalpy values were less than 40 kJ mol -1 (i.e., 20.3 kJ mol -1 and 31.3 kJ mol -1 for GW and AGW, respectively), revealing that the process of adsorption of Rhodamine B laid in the physisorption range. The positive value of entropy confirmed the arbitrariness at the solid-liquid interface, reflecting the affinity of the adsorbent surface. Table 7 summarized the adsorption capability of various adsorbents, at an optimal dosage and pH level. In this present research, the high comparable capacity for the removal of Rhodamine B was 54 mg g -1 and 72.4 mg g -1 for grass waste and activated grass waste, respectively. This maximum uptake reflects the maximum surface active site for adsorption in comparison to waste biomass materials, including orange and banana waste powder.

Conclusion
Adsorbent based on grass waste was synthesized, and its efficiency in the removal of Rhodamine B from aqueous phase was studied. The process parameters have a substantial effect on the pollutant removal capacity of the adsorbent. The spectroscopic analysis confirms the successful removal of chlorophyll and limonene as a result of alcoholic wash during the activation process. Metallic impurities were also leached out during acid treatment, which is clearly perceptible in the EDX analysis. However, the thermal stability of the activated grass decreased due to the chlorophyll removal, which binds lignin chains in the grass. The adsorption process of Rhodamine B onto GW and AGW is endothermic, and tends to be more spontaneous at a higher temperature. The enthalpy of adsorption was less than 40 kJ mol -1 for both GW and AGW, suggesting that the adsorption may be classified as physisorption. Kinetic analysis showed that the adsorption of pollutant dye was diffusion-controlled. The value of the maximum adsorption capacity obtained from the Langmuir isotherm model was 54 mg g -1 and 72.4 mg g -1 for GW and AGW respectively. Keeping in view the adsorption results, adsorbent synthesized from waste grass could be considered as an alternative to adsorbents for the treatment of colored water.

DATA AVAILABILITy STATEMEnT
The authors confirm that the data supporting the findings of this study are available within the article [and/or]

ConFLICT oF InTEREST
The authors declare that they have no conflict of interest.