Adsorptive Separation of Brilliant Green Dye from Water by Tartaric Acid-Treated Holarrhena antidysenterica and Citrullus colocynthis Biowaste

Holarrhena antidysenterica (Ha) and Citrullus colocynthis (Cc) biowaste from indigenous Pakistan resources was used to remove toxic brilliant green (BG) dye from aqueous solutions in a batch mode. Tartaric acid chemical modification gave promising results than the nonmodified forms of biowaste. Surface characterization was carried out by FT-IR and SEM.,e optimum conditions for (BG) dye elimination by Ha-tartaric acid modified (Ha-Ta) were 1.8 g, 45 minutes, 4.0 pH; 40°C, and 100 rpm and with Cc-tartaric acid modified (Cc-Ta) were 1.6 g, 45 minutes, 6.0 pH; 40°C, and 150 rpm dye solution shaking rate, which gave optimum results. Equilibrium data of raw and chemically modified biowaste followed the Langmuir model indicating monolayer chemisorption. Qmax values were found to be 55.24mg/g, 112.35mg/g, 50.50mg/g, and 79.36mg/g for Ha, Ha-Ta, Cc, and Cc-Ta. Kinetics followed the pseudo-second-order kinetic model. Dye removal involved surface and intraparticle mode of diffusion. ,ermodynamic studies proved the process to be spontaneous and exothermic one. ,e adsorbents can be effectively utilized for the removal of toxic basic dyes, such as BG from wastewaters.


Introduction
With the advent of modernization came great responsibilities to meet the needs of mankind. Increasing industrialization resulted in pollution of soils and water. Textile, paper, and leather industries discharge dyes directly into the water bodies without any pretreatment, leading to environmental concerns. Dissolution of particle charges in an aqueous medium categorizes dyes into anionic (acidic, direct, and reactive), cationic (basic), and nonionic (dispersed). In addition, cationic colorants are more hazardous than anionic ones [1,2]. Dyes are tolerant to microbial, chemical, and photochemical degradation. eir presence in minute amounts (1 mg/L) [3] poses allergic, mutational, and carcinogenic disabilities [4]. Classical methods such as precipitation, ozonation, coagulation, flocculation, ion exchange, and reverse osmosis [5] proved to be limited to smaller scale, poisonous sludge productivity, and expensive procedures, urging scientists to opt for new pathways [6]. Adsorption is favored upon them due to simple design, availability, maintenance, cost effectiveness, easy operation, and economic feasibility. It offers strong competitors against activated carbon, which is immensely utilized for its chemically active nature, higher specific surface area, larger pore volumes, and adsorption capacities [7], but when prepared from coal and lignocellulosic ingredients, it is ultraexorbitant and not ecofriendly [8,9].
Adsorption is termed as removal of impurities (adsorbates) from the solid surface (adsorbent) by establishing strong bonding among the porous structure of the adsorbent surface and chelated entities, the adsorbate particles being eliminated from the bulk phase while moving from one phase to another crossing a barrier. Complexation is followed by ion exchange, hydrogen bonding, and pore diffusion [10,11]. Low-cost materials such as fallen leaves, bagasse, seeds, saw dust, fruit peels, and tree bark are used as adsorbents because of cheapness and availability.
Brilliant green (BG), a synthetic organic coloring agent, belonging to the triphenyl methane family is widely used in printing paper and textile industries [12]. It causes serious health issues, damaging renal tissues and the reproductive systems in humans. Its decomposition results in serious environmental damage by producing oxides of nitrogen and sulfur [13]. Recently, dye removal was performed by nanofibrous composites [14], photocatalysis [15], electrocoagulation [16], microwave-induced catalytic oxidation [17], biodegradation [17], membrane separation [4], advanced oxidation processes [18][19][20][21], and adsorption [22] techniques. e adsorbents used are Holarrhena antidysenterica (Ha) and Citrullus colocynthis (Cc). H. antidysenterica (Inderajao) has many medical uses as a cure for dysentery, skin inflammations, osteoporosis, and rheumatism [23]. Various functional moieties [24] such as cellulose, hemicellulose, and lignin are present that encapsulate BG from wastewaters. C. colocynthis (Indrayan) cures breast cancer and diabetes and increases hair length [25] due to various natural products in it [26,27]. e aim of this study is to utilize cheap biowaste from indigenous Pakistan resources. ey are modified with tartaric acid (C 4 H 6 O 6 ), to remove toxic brilliant green dye from aqueous solutions. e raw and modified adsorbents are characterized by Fourier-transform infrared (FTIR) spectroscopy and scanning electron microscopy techniques. Batch adsorption studies were performed. Effects of various experimental parameters such as adsorbent dosages, pH effects, temperature studies, agitation rates, and contact times were investigated. Isothermal, kinetic, and thermodynamic studies were conducted for evaluation of the possible mechanism involved.

Collection of Biowaste.
Ha and Cc biowastes were taken from markets of Lahore city, Pakistan. ey were washed, dried in sunshine for 3-4 days, grounded, and stored in plastic jars after passing through 60 mesh sieves. e resultant product was soaked separately in 10% aqueous solution of tartaric acid for chemical modification, then filtered, and dried again prior to usage [27]. 2.3. Chemical Modifications on Adsorbents. 5 g adsorbents were added to 25 mL of acidic, basic, and chelating solvents and kept for 4 hours, resulting in filtrates, which when treated with BG dye gave the desired concentrations [28].

Biosorption Experiments.
Batch scale studies were carried out for all the parameters. 100 mL BG dye solutions were taken in 250 mL conical flasks at ambient temperatures. Fixed amounts of adsorbents were added to the dye solutions, then kept in rotary shakers, and agitated for 120 minutes. Various adsorption parameters such as adsorbent dose (0.2-2.2 g/L) [29], pH (1-10), specific contact time (5-60 minutes), agitation speeds (20-200 rpm), and temperature (303, 313, 323, 333, 343, and 353 K) were studied. Dye concentrations were monitored in filtrates, using a UV/ Vis spectrophotometer [30]. Percentage adsorption (% R) of dye was calculated (equation (1)), and the concentration of dye retained per unit mass of adsorbent is given by equation (2): where C o is the initial BG concentration (mg/L) and C e is adsorption at equilibrium (mg/L). Also, "q e " is the adsorption capacity of BG (mg/g), "V" is volume of the solution (L), and "m" is the amount of adsorbent used (g) [31]. All experiments were performed twice, and average values were considered for this study.

Adsorption Kinetics.
Rate of reaction is used for designing the mechanism of adsorption by finding conditions which best fit the models for a specific adsorbent-adsorbate system. Usually, systems follow Lagergren pseudo-first-order (equation (3)) or pseudo-second-order (equation (4)) kinetic models [32][33][34][35]: where k 1 (h −1 ) and k 2 (g/mg.h) are rate constants for the pseudo-first order and pseudo-second order kinetic models, respectively, q t (mg/g) is the amount of adsorbate adsorbed at time t, and q e (cal) (mg/g) is the amount of adsorbate adsorbed at the equilibrium state. Ho and Mckay explained the independency of particle diameter of the pseudo-rateconstant in chemically controlled dye uptake; hence, flow rate will be dependent upon the ionic concentrations of the solutions. A plot between ln (q e − q t ) and t demonstrates a linear relation for the applicability of the pseudo-first-order model. R 2 figures are used for the evaluation of the best-fit model. Pseudo-second-order modeling is demonstrated by both basic and acidic dyes. A linear plot among t/q and t confirms this model. e Elovich model represented in equation (5) gives energy variations exponentially related to fluctuations of adsorbent sites. Applied to gas adsorption on solid surfaces, this model implies multilayered adsorption [36,37].
Linear plots are obtained by plotting ln t (minutes) at the horizontal axis along with qt (mgg −1 ) at the vertical axis. Significant checking of the kinetic modeling utilizes P (percent-relative deviation) values (equation (6)). Lower values of P indicate more appropriateness of kinetic data.
where q e (exp) (mg/g) is the experimental biosorption capacity and q e (mg/g) is the calculated biosorption capacities and N represents the number of estimations used for the experiment [38]. 25 mg/L dye solutions were selected at 298 K with all optimized conditions for BG retention kinetics. Absorbance values were seen at a difference of 5 minutes. e upper buoyant film of the dye solution was selected where the speed of adsorption was rapid in the earlier stages as compared to the later ones, where it came to a gradual decrease as equilibrium arrived.

Adsorption
Isotherm. e design and mechanism of a biosorption system for removing dyes from wastewater requires finding of most accurate correlation for the equilibrium curve. us, the correlation among the adsorbate and adsorbent is performed by studying the distribution of the dyes among the solid-liquid phases at equilibrium. 10,15,20,25,30,35, and 40 mg/L concentrations of BG dye in a 250 ml stoppered conical flask were selected for isothermal studies along with optimum conditions of temperature, pH, adsorbent dose, contact time, and agitation speed. It determines the characteristics of the adsorbent's surface, its capacity, and mechanism of the underlying process [13]. e isothermal study in this work was conducted by using Langmuir, Freundlich, Temkin, and D-R isotherms. e most popular isotherm is the Langmuir isotherm. According to this isotherm, there is a finite number of active sites, homogeneously distributed over the adsorbent's surface area and having the same affinity for adsorption of a monolayer, with no interaction among adsorbed molecules. Its linear form is [39] 1 where b is called the Langmuir constant (L/mg); q e � amount of adsorbate adsorbed at equilibrium (mg/g); q max � maximum monolayer uptake ability of the adsorbent (mg/g); and C e � equilibrium impurity absorption in solution (mg/L). R L is the separation factor, calculated from Langmuir constants, and C o � the initial concentration of the dye (mg/g), as shown in the following equation [40]: e value of R L displays the isothermal studies to be unfavorable (R L > 1), linear (R L � 0), favorable (0 < R L < 1), or irreversible (R L < 0). A graph between 1/q e and 1/C e displays the desired results.
Another popular model is the Freundlich isotherm. Physisorption (physical adsorption) of adsorbates on the adsorbent layer enhances interactions among adsorbed particles favoring heterogeneous, multilayer adsorption on exterior rough surfaces [41]: where K f represents the binding constant and n is the adsorption strength. Figures of "n" in the range of 1-10 display a good adsorption procedure [42][43][44]. is model as compared to multi-ions best describes a larger ionic concentrate, involving single-dye ions, where selectivity along with interferences of the ions prompts for other models. e graph of log q e vs. log C e shows the results. e Temkin isotherm model considers reduction of adsorption heat in a linear manner and uniform distribution of binding energies during adsorbent-dye reactions [42,45].
where A T �constant related to adsorbate-adsorbent at equilibrium (L·g −1 ) and B T � Temkin constant associated to heat of adsorption (J·mol −1 ) Nature of binding forces based on B T values imply that values lower than 8 demonstrate a weak physisorption process, while numbers higher than 8 are responsible for a strong chemisorption process among the adsorbate-adsorbent molecules [46,47]. Linear plots of q e against lnC e aid in determining of the sorption heats B T and biosorption potentials A T values. e D-R isotherm demonstrates the adsorption process considering Gaussian energy distributions onto both homogeneous and heterogeneous surfaces [48,49] for intermediate concentration ranges. It represents the total free energy along with physical or chemical characteristics of the adsorption process expressed as follows: E is the mean free energy whose values are calculated by considering "β" (mol 2 /J 2 ).
. (13) e inference of the adsorption process is based on E values where a value lower than 8 kJ/mol represents physisorption, and an intermediate range of 8 to 16 kJ/mol shows an ion-exchange reaction and above 16 kJ/mol demonstrates a chemisorption one [40]. Linear plots of lnq e vs Ɛ 2 provide the desired results.

Characterization of Adsorbents.
e suitable chemical used for chemical modification was selected by using different chemically modified biowastes for removing BG dye in the batch mode as shown in (Figure 1), and results indicated that tartaric-acid-modified adsorbents had shown best results. It is because BG is basic in nature, so it reacts more with acid-modified biowaste. So, further studies were carried out with tartaric-acid-modified biosorbents.
Both unmodified and modified biowastes were used separately for removing BG dye. e obtained results are as follows [50].

Chemical Treatment.
Pretreatment can be carried out by a variety of methods using acidic (hydrochloric acid, citric acid, tartaric acid, sulfuric acid, and nitric acid), basic (sodium carbonate, sodium hydroxide, and calcium hydroxide), chelating (ethylenediamine and epichlorohydrin), or oxidizing (hydrogen peroxide) agents [51]. Chemical treatment ensures uniformity in ionic distributions, reducing moisture levels that guarantees lower decomposition of the entities. Moreover, acid and basic treatment enhances protonation, ester bonding, and higher micropore proportions, leading to early attainment of equilibrium [27,[52][53][54][55]. Tartaric acid was selected as the chemical modifier as it yielded the highest percentages of dye removal as shown in Figure 1.

Fourier-Transform Infrared (FTIR) Analysis.
Surface morphology describes about the material geometry, topology, and surface structure. e geometry ranges from microscale to the mesoelements and their ordered as well as complexed shapes. e topology describes the connection between micro-and mesoscale elements. e rough surfaces possess complex features upon close inspection, and their characterization gives us deep insights about the material's microstructure along with effective properties [56]. FTIR helps in the molecular composition, structure, and energy-level transitions of unknown surfaces and layers close to it. It is employed when samples are subjected to infrared radiations and bonds between diverse elements absorb light at different frequencies [57]. Group frequencies applied to most compounds having that particular functional group along with skeletal vibrations, unique to specific molecules, are combined to identify the unknown compounds. ese are carried out by visual comparison or computerized searching, where the adsorption band is in proportion to number times of occurrence of the functional groups within the molecule [58]. e functional groups that are responsible for elucidation of BG dye from the adsorbent surfaces are determined by it. BG-dye-loaded Ha spectra were studied (Figure 2     Journal of Chemistry adsorbents. From the images, it can be seen that hollow spaces [61] are present among the rigid, spherical edifices [5] of Ha, which facilitated the adsorption of BG dye through physisorption. Acidic treatment resulted in the svelte, etched structures consisting of multifold channels providing more potential sites for BG adsorption [27]. e Cc adsorbent changed from flaky with voids to large agglomerated and bean-like structures attached to the surface when esterification was performed [27].

Batch Adsorption Studies
3.5.1. Effect of Adsorbent Dosage. Adsorbent dose is an important parameter in analyzing the efficiency of the adsorption process. It was calculated by utilizing the dose from 0.2 g-2.2 g with 25 mg/L dye solution in 250 mL stoppered Erlenmeyer flasks for both untreated and acid-treated Ha and Cc adsorbents, as shown in Figure 4(a). For Holarrhena antidysenterica, the adsorption increased up to 2 g with 96% dye removal as compared to Citrullus colocynthis, which gave 94% dye removal at 1.8 g. Tartaric acid modification increased the availability of active surfaces incorporating additional functional moieties of carboxylic and hydroxyl groups leading towards greater dye adsorption than the raw ones, hence leading to 99% removal at 1.8 g for modified Ha and 96% removal at 1.6 g for treated Cc. After that, equilibrium rise in concentration leads towards the overlapping of saturated sites and rise in diffusion path lengths [62]. Increase in mass per unit area rises the concentration gradient at higher concentrations resulting in higher BG dye removal [2,63].

Effect of Contact Time.
Adsorption improved with rise in contact time until an optimum contact time was achieved [50]. A period of 1 hour with a 5-minute interval was selected utilizing 250 mg/L dye solution in 250 mL flasks. Figure 4(b) displays the relative effect of contact time on raw and modified adsorbents. Adsorption rose in early stages as abundance of active surfaces are available, while repelling of adsorbed-unadsorbed moieties resulted in decline at later stages, when molecules penetrate the internal surface [64]. e optimized contact time was 50 min for both Ha and Cc, with a percentage of dye removal of 89.35% for Ha and of 84.84% for Cc. After chemical modification, the dye adsorption was seen to be 97% at 45 minutes for modified Ha as compared to 93% at 45 minutes for modified Cc. e driving forces among the liquid and solid phase help in counteracting of the mass transition resistance among the dye molecules [2,65].

Effect of pH.
Solution pH controls electrostatic charges and the speciation of adsorbates [66]. e magnitude demonstrated by the charged species of the dyes results in variance of speed of adsorption.
e point of zero-charge pHpzc, where the negative and positive sites are equivalent [67,68], was determined by the electrochemical method [69] as described in our previous studies [27]. Ha gave a pHpzc of 6, and Cc gave 5. Mainly, it  is observed that, at acidic pH, the adsorbent surface is more positive because of protonation of active sites; hence, decrease in biosorption of basic dyes occur [2,66], whereas at alkaline pH, due to deprotonation, more -OH ions hinder anionic dyes adsorption, due to the repulsive forces as the adsorbent surface appears to be negatively charged.
Monitored in pH (1-10), 25 mg/L dye solution in 250 mL stoppered conical flasks, the results (Figure 4(c)) display the best removal (%) of BG dye for Ha at pH 7 (95.44%) and Ha-Ta (98.83%) at pH 4 and for Cc at pH 7 (98%) and Cc-Ta (99.5%) at pH 6. e increased removal of BG dye in the Ha-Ta and Cc-Ta cases is due to the chelation forces, which appear in the case of modified adsorbents. BG, a basic dye existing in the form of positive charged species on the surface of Ha and Cc, plays a significant role, as the adsorbents are solely dependent upon solution pH for adsorption.
Excessive H + ions from the protonated forms of carboxyl groups compete with the cationic moieties in the dye for vacant adsorption sites, imparting repulsive forces among the dye and adsorbent surfaces [67,70]. Hence, decrease in hydrogen bonding occurs; however, at higher pH, as observed in Ha and Cc, positive charges are reduced at the adsorbate-adsorbent interface and negative charges of COO − groups of the adsorbent dominate, resulting in enhanced dye removal through electrostatic forces of attraction [9].

Effect of Temperature.
Temperature generates the energy required to conquer the mass transfer barrier present among the dye solution and adsorbent potential sites. A range of 30-80°C was selected for temperature studies, as shown in Figure 4(d). At 50°C, a percentage removal of 88.83% was observed for Ha and 93% for Cc. Tartaric acid treatment yielded maximum adsorption of 99% for modified Ha and 96% for treated Cc at 40°C. Biosorption increased with an increase in temperature, favoring the increase of entropy that strikes the color moieties against the potential binding surfaces, which leads to an increased speed of the process; also, the inflammation of adsorbent sites increased the active sites of the biological material, resulting in a larger amount of dye removed. An increase in the porosity of pore volumes of adsorbents rises the kinetic energy for better dye removal [2].

Effect of Agitation Rate.
Agitation rate determines the distribution of solute particles in the bulk solution and the outer exterior film formation; the 20-200 rpm range was chosen during experimentation. At 100 rpm 89%, dye removal was demonstrated for Ha which rose up to 96% for the acid-treated forms while Cc removed 84% dye at 150 rpm, which rose towards 91% for modified forms (Figure 4(e)). Increase in agitation rate improved BG interactions with the active surfaces of the adsorbent, reducing the resistance of the external boundary sheet and raising mobility. Also, the external mass transfer coefficient increased; thus, better adsorption of the dye molecules was achieved [71]. Increased agitation speed produces higher centripetal force among the dye molecules that imparts repulsion among them, overcoming binding forces, and the mechanism shifts towards desorption [2].

Adsorption
Isotherm. An adsorption isotherm was conducted using Langmuir, Freundlich, Temkin, and D-R isotherms. Results are presented in Table 1 along with graphs in (Figure 5). e values of correlation coefficient R 2 are in close proximity to the one confirming the Langmuir isotherm model to be in complete agreement for adsorption of BG onto both the adsorbents. Q max for Ha and its modified forms were greater, implementing adsorption of BG better than Cc and its treated forms. Also, it is seen that the biosorption process is monolayer, homogeneous, and followed the chemisorption process, inhibiting any side reactions within molecules [72]. R L figures for the adsorption of BG on raw and modified adsorbents were less than one, showing a favorable biosorption process [13,73].
e b values indicate significant affinities of biosorbents for BG dye removal [13]. Freundlich isotherm's results present that R 2 values were lesser than that of Langmuir, indicating lesser chances for the physiosorption mechanism. Moreover high charge to mass ratio as well as advanced chelation abilities of BG molecules lead towards better binding capacities of the modified forms. Furthermore, lower values of regression coefficients render the experimental fitting towards the Temkin isotherm. For D-R isotherms R 2 values were seen to be lesser than other isothermals, and E values favored the physisorption process. Q m values of the modified forms were higher than the raw ones.

Adsorption Kinetics Studies.
e outcomes of the kinetic modeling are displayed in Figure 6 and Table 2. From the data obtained, it can clearly be illustrated that the pseudosecond-order equation seems to be the most accepted model for BG adsorption on raw and modified forms of adsorbent as evident from R 2 depicting the chemisorption process indicating covalent boding through sharing or electron transferring. A larger variance of P values is observed among the experimental and calculated values for the pseudo-firsorder kinetics as compared to the second order, hence rendering it ineffective against the pseudo-second-order, where the difference among P values are far less. Also, a rise in initial sorption rates "h" and decrease in half-lives "t 1/2 " were observed from moving from the raw towards the modified forms [52,74]. In the Elovich model, binding rate "a" increased for the acid treated while R 2 displayed a lesser fitting.

Mass Transfer Parameter.
Removal of BG dye on raw and modified adsorbents was rapid in the initial stages and slow in the preceding time. is is carried out by either the boundary-layer diffusion mechanism or intraparticle diffusions. e adsorption process involves (a) film diffusion, transfer of adsorbate towards the solid adsorbent, (b) intraparticle/pore diffusion, diffusion takes place from external to internal pores, and (c) formation of complexes      among the dye and functional moieties in the adsorbent [34].
is model was introduced for the realization of the mechanism [75].
e Webber and Morris equation is as follows: where k id is the coefficient of intraparticle diffusion. Linear plots of qt against t 1/2 intersecting origin favor intraparticle  diffusion; however, if the data exhibit multilinear plots, then two or more steps are involved. e initial steps are (a) transportation of the dye from the bulk liquid solution to the external boundary surface, (b) diffusion of the liquid film, and (c) particle diffusion within the pores of the adsorbate. Figure 6 displays the dual nature of the model with the curved followed by straight paths, for varying adsorption extents, in the initial and final stages of the experiments. is shows boundary-layer diffusion at initial stages and intraparticle at later stages [76]. e "C" values of thickness of borderline exterior walls were seen to be rising for the modified forms as compared to unmodified ones as implicated by carboxyl and hydroxyl groups on the adsorbent surface leading towards a complex biosorption mechanism [77]. Complete parameters of the intraparticle diffusion model are represented in Table 2.
For the prediction of the actual mechanism involved in the adsorption process, Boyd plots were used to check whether film diffusion or intraparticle diffusion were the rate-determining steps. Fractional achievement of equilibrium with variation in time is known to be the boundarylayer diffusion mechanism. Boyd expression is shown in equation (15), and fractional equilibrium is shown in equation (16): where B b � Boyd constant and F � fractional achievement of equilibrium at time t, where F � q t q e . (16) e intersection of the plots through the origin confirms the Webber-Morris plots, while the boundary layer is the mechanism involved if the intersection is not observed. Graphs between Bb and t are shown in Figure 6 implying the boundary-layer diffusion mechanism or chemical reaction as the rate-determining approach [2,66]. K fd values are shown in Table 2 clearly indicating the higher R 2 values than the intraparticle diffusion.
3.10. Error Calculation. In this study, nonlinear regression error function and RMSE values (equation (24)) were also calculated to check the variation of experimented and calculated values, and the least error gave the most promising equilibrium and kinetic model [79].
where q e (cal) (mg g −1 ) is the calculated value and q e (exp) (mg g −1 ) is the experimental value, at any instant t, and N is data points. e Langmuir model was seemed to be followed by the raw and modified forms except for the BG with CC, which confided with the Freundlich model. e pseudosecond-order model was found to be most appropriate by displaying the highest regression and least error values ( Table 2).

ermodynamic Studies.
ermodynamic studies undergoing within the biosorption process were evaluated by equations (25)- (27), and the obtained results are presented in Table 3 along with graphs in Figure 6 [40].
where K d is the equilibrium constant, q e (mg/g) is the amount of dye adsorbed, and C e (mg/L) is the concentration of the solution at equilibrium, respectively. (ΔG°) represents Gibbs free energy, ∆H and ∆S are the heat and entropy changes accompanying the adsorption process, R is the universal gas constant (8.3143 J/mol/K), and T is the temperature in (K). Negative (ΔG 0 ) values implicit a favorable and spontaneous process; also, values of K d increased with rise in temperatures indicating favorable adsorption [80]. Negative values of (ΔH 0 ) display the exothermic nature [66], and (ΔS 0 ) positive values illustrate the elevation of disorderness of the adsorbent-adsorbate interphase within the adsorption process [2]. e Arrhenius equation determines the activation energy: where A is the frequency factor, R is the gas constant (8.314 J·mol −1 ·K −1 ), k (h − 1) is the constant rate, and T is the absolute temperature (K). e observed values indicate the reaction to be a physisorption.

Adsorption
Mechanism. e surface of the adsorbent, as evident from the FT-IR analysis, possesses cellulose, lignin, and hemicellulose constituents (Figures 2(a)-2(d)) that contain carboxyl and hydroxyl functional moieties. BG dye and Ha/Cc adsorbents are both solvated in water and require rupture of hydration shells for the dye to be adsorbed, hence forming both outer-(nonspecific) and inner-sphere (specific) complexation with the adsorbent. e IR spectrum confirms the whole molecule within the interlamellar space of the adsorbent, also evident in aggregated structures in SEM images. Chemical modification increases the surface porosity and reduces cellulose crystallinity during the esterification reaction. e reaction further exposes inter-and intramolecular hydrogen bonding within the cellulose towards the dye which incorporates within the aggregated cavities during dye adsorption. Outersphere complexes occurs at the organic surface of the adsorbents where the amino group of cationic BG forms electrostatic attractions with the COO� groups of the adsorbents. Free lone pairs on nitrogen atom also form hydrogen bonding with OH�groups on the adsorbent. Chemical interactions such as π-π interactions among the aromatic part of the dye and the oxygen plane of the adsorbent lead towards the inner-sphere complexation. Moreover, sp 3oxygen-containing functional groups pose structural defects on the adsorbent surface [81][82][83] that facilitate further penetration of the dye towards the micro-and macroporous sites. Hence, boundary-layer diffusion along with intraparticle diffusion occurs into the inner cellulosic layers of the biosorbent. Film distribution is the rate-controlling step as indicated from the kinetic studies. e complete mechanism is displayed in Figure 7 [81]. Similar results are shown in [2,81].

Comparison of the Adsorption Capacity of Adsorbents
with the Literature. A comparison of maximum adsorption capacity of both the adsorbents, in raw and acid-treated forms, is carried out with other alternative bioadsorbents and represented in Table 4. e qmax calculated for Ha, Cc, Ha-Ta, and Cc-Ta was found to be 55.12, 112.3, 50.5, and 79.36 mg/g, respectively. Hence, the adsorbents yield higher adsorption capacities than most of other adsorbents and can be used for the effective removal of BG dye from wastewaters.
From the literature study, it is seen that any other researcher has not reported removal of BG dye from the abovementioned adsorbents. It is the first research where tartaric-acid-treated Ha and Cc adsorbents are used in batch modes for the removal of BG dye, hence establishing the novelty of this work.

Regeneration Study.
Regeneration studies were carried out in three consecutive cycles, and the third cycle still poses 87% of dye adsorption of BG-Ha. Cc gave 87%, while the modified forms gave 88% for Ha-Ta and 89% for Cc-Ta. Future research is needed to carry out an adsorption procedure employing these adsorbents for metal sequestration, activated carbon preparation, microwave solid degradation, and removal of other organic pollutants. Hydrogen bonding

Conclusions
e study carried out demonstrates that both H. antidysenterica and C. colocynthis are inexpensive, environmental-friendly biowaste for the efficient adsorption of dyes from waste waters. e biowastes were treated with tartaric acid, which incorporated the positively charged moieties increasing the dye-removal ability.
e characterization techniques demonstrated the presence of -COOH and -OH groups that aid in BG dye adsorption by electrostatic attractions, hydrogen bonding, and π-π interactions. e mechanism is evident of transforming of particles towards the exterior of the surface, followed by shifting of ions within the solution from the exterior surface towards the interior. e adsorption takes place at surfaces with assistance of carboxyl, hydroxyl, and amino groups. At the last stage, the boundary layer and Webber-Morris plots are prevalent into the interior space. Film diffusion along with intraparticle diffusion is the rate-determining step. Isothermal studies, such as Langmuir, Freundlich, Temkin, and D-R models, were checked, and the Langmuir model succeeded with the maximum monolayer adsorption capacities for BG dye removal of 112.50 mg/g for Ha-Ta and 79.36 mg/ g for Cc-Ta. ermodynamic analysis proved that the adsorption process is exothermic and spontaneous accompanied by increasing entropy. Both raw and modified adsorbents followed the pseudo-second-order kinetic model as evident from kinetic studies.

Data Availability
All related data are mentioned in the manuscript with references.

Conflicts of Interest
e authors declare that they have no conflicts of interest that can influence the work reported in this paper.