Adsorption of Pesticides Using Wood-Derived Biochar and Granular Activated Carbon in a Fixed-Bed Column System

: Pesticides have great potential to contaminate resources of drinking water by perco-lating and leaching, when applied in the agriculture sector as well as in domestic region. Activated carbon (AC) and Biochar (BCH) were used for adsorption in a ﬁxed-bed column system. Both of the adsorbent-packed columns indicated an increase in the breakthrough time for atrazine from 3350 to 5800 min and 3200 to 5700 min, chlorothalanil 3200–5600 min and 3150–5550 min, β endosulfan 3050–5400 min and 2950–5400 min, and α -endosulfan 2900–5200 min and 2850–5200 min with bed heights from 10 cm to 15 cm, respectively. Similarly, when ﬂow rate increased from 0.5 to 1.5 mL min − 1 and contaminant concentration from 50–100 µ g L − 1 , it resulted in a decrease in exhaust time. The models of Yoon–Nelson (R 2 = 0.9427) and Thomas (R 2 = 0.9921) describe the process of adsorption to be best well-under optimal conditions. Both the adsorbents would be efﬁciently utilized as the best adsorbents to remediate pesticide-contaminated water under optimal conditions. Pesticides adsorption onto adsorbents followed the order of atrazine > chlorothalanil > β -endosulfan > α -endosulfan.


Introduction
Pesticides have a significant role throughout the world in the field of food production and farming [1]. Pesticides are a substance utilized to deter, eradicate, kill, or diminish pests; to regulate the growth of plant [2]; and to prevent loss to yield of crops [3]. After application of pesticides, rainfall or irrigation water carries pesticides residues to the nearby surface and ground water bodies through runoff or percolation [4,5], contaminating water resources and consequently deteriorating drinking water quality [6]. Due to their nonbiodegradable, carcinogenic, persistent, and toxic nature [7], pesticides have undesirable Atrazine (58% purity), chlorothalanil (33% purity), β-endosulfan, and α-endosulfan (47% purity), were purchased from local market manufactured by FMC United (pvt.) Ltd. and were utilized as adsorbates. Stock solutions of 1000 µg L −1 of all the four pesticides were prepared in deionized water, from which further 12 µg L −1 working solutions were prepared, composed of all the four pesticides to be used in the column experiment. Diluted HCl and NaOH (Riedel-de-Haen, Seelze, Germany) was utilized to regulate the pH, and buffer solutions of pH-3, 5, 7, 9, and 11 were prepared and used to maintain the specific pH of the solution. Hard wood (Dalbergia sissoo) was used to prepare BCH in a dry muffle furnace (Shanghai Haoyue Technology Co., Ltd., Shanghai, China) through the process of pyrolysis. The furnace temperature was programmed to rise slowly at a rate of 2 • C min −1 until the desired temperature of 500 • C was achieved (selected as a typical mid-level pyrolysis temperature) for 6 h under a very low continuous flow of nitrogen at a rate of 150 to 200 cm −3 min −1 . Once the desired temperature was obtained, the flow of nitrogen was stopped [39]. AC applied in the study was purchased from Norit Nederland BV Amersfoort. All chemicals used in the study such as n-hexane, dichloromethane, NaOH, HCl, and Na 2 SO 4 (Riedel-de-Haen) were analytical grade. Prior to each experiment, all the glassware were washed with dichloromethane and deionized water was used for washing repeatedly.

Equipments
For pH measurements, a pH meter-1120-manufactured by Mettler-Toledo GmbH Process, Postfach, 8902 Urdorf, Switzerland-was used. Gas chromatographic mass spectrophotometry (GC-MS Shimadzu, 2010, Kyoto, Japan) was used for determination of pesticides. The analysis of FTIR (IR model Shimadzu 8201, Kyoto, Japan) and X-Ray diffractometry XRD model JDX-3532 were used to examine spectral characteristics of AC and BCH. Surface morphology was investigated by the help of scanning electron microscopy (SEM) model JSM 5910 JEOL, Tokyo, Japan.

Fixed-Bed Column Experiment
The experiment of fixed-bed column was performed in a 2.8 cm-diameter, 40 cm-height glass column for the determination of AC and BCH dynamic adsorption characteristics, for removal of pesticides. The experimental fixed-bed column graphical diagram is presented in Figure 1. The experimental setup includes teflon tubing, feed storage, glass column, peristaltic pump, and a sample collector. In the entire experiment, the glass column was packed with each adsorbent bulk volume and about 2 cm (height) of glass beads. For uniform flow and effluent blockage prevention, glass wool small volume was added at the lower and upper ends of the glass column. During performance of all tests, a stable room temperature of (25 ± 2 • C) was maintained. The impact of flow rate (0.5, 1, 1.5 mL min −1 ), bed height (10, 15 cm), and influent initial concentrations (50, 75 µg L −1 ) were examined on the process of adsorption by the breakthrough curves (C/Ci changes versus time, where Ci and C represent the influent and effluent concentrations of the aqueous solution, respectively [40,41]. The adsorption capacity for pesticides uptake, represented as qe (mg/g), was determined through the following equation: where Ci = initial pesticides' concentration (µg L −1 ), Cf = final pesticides' concentration (µg L −1 ), V = volume of the solution, and W = weight of the adsorbent (g).

Thomas Model
The most frequently applied Thomas model is used for the prediction of breakthrough curve and determination of column adsorption efficiency. Value of the adsorbent maximum adsorption capacity is significant to design adsorption column, and for assessment of adsorbent adsorption capacity. Thomas' model has been used in a continuous column study. This model is suitable where the rate limiting steps for adsorption are not dependent on internal and external diffusion [42]. Following is the general expression of

Thomas Model
The most frequently applied Thomas model is used for the prediction of breakthrough curve and determination of column adsorption efficiency. Value of the adsorbent maximum adsorption capacity is significant to design adsorption column, and for assessment of adsorbent adsorption capacity. Thomas' model has been used in a continuous column study. This model is suitable where the rate limiting steps for adsorption are not dependent on internal and external diffusion [42]. Following is the general expression of the model: whereas, at time (t), C f is the effluent pesticides concentration (µg L −1 ) and C i is the influent pesticides concentration (µg L −1 ). Thomas' model rate constant is represented by k Th (L min −1 mg −1 ) and the adsorbent's adsorption capacity by q 0 (mg g −1 ), while (t) expresses the total time of flow (min). Quantity of adsorbent packed in a column is represented by W (g) and rate of flow by Q (ml min −1 ). The values of k Th and q 0 can be attained by plotting the graph amongst ln [(C i /C f ) − 1] and (t).

Yoon-Nelson Model
Yoon-Nelson is the simplest model, which describes that the molecule of adsorbate reduction rate possibility is directly proportional to the possibility of adsorbate breakthrough and adsorption onto the adsorbents [43][44][45]. The model general equation is as follows: where K YN stands for Yoon-Nelson rate constant (min −1 ). Required time (min) for 50% breakthrough of pesticides is represented by τ; t represents processing time in (min). Values of K YN and τ are obtained by plotting (C t / (C i − C f ) vs. (t) to determine the plot slope and intercept.
2.6. Analytical Method 2.6.1. Extraction of Pesticides The obtained filtrates were extracted by liquid-liquid extraction method [46]. Briefly, in a conical flask, 40 mL of filtrate, 12 mL of solvent n-hexane, and 4 g of NaCl were taken and shaken at 80 rpm for 1 h in a horizontal shaker (Bremen, POB 105363, Bremen, Germany). Few drops of phosphate buffer were added to adjust pH to 7 and, if necessary, diluted HCl or NaOH would also be added. The filtrate was collected in a separatory funnel and was held until the creation of two distinctive layers. The n-hexane layer was collected as a filtrate and was washed two times by addition of 2.4 mL n-hexane solvent. To remove water particles from the separated layer, sodium sulphate (Na 2 SO 4 ) was added. Once the contents were separated through separating funnel, it was evaporated at 25 • C on a rotary evaporator to reduce the volume to 1 mL. Reference material and sample blanks were also used to verify the precision and accuracy of the analysis and extraction processes.

GC-MS Chromatography
The saturated organic solvents were collected in 1-mL GC-MS vials and placed in GC-MS Agilent port for determination of the pesticides by gas chromatograph. A gas chromatograph mass spectrophotometer was used for analysis, equipped with a splitless mode injector system, a flame photometer detector, and a capillary glass column of 5 MS TRB with 30 m-length, an internal diameter of 0.25 mm, and stationary film thickness of 0.25 µm, manufactured from Phenomenex, which was used for pesticides determination. The temperature of the oven was held for 1 min at 50 • C; then, at 25 • C min −1 programmed to 125 • C; from 125 • C to 200 • C at interval rate of 10 • C min −1 ; from 200 to 270 • C at interval rate of 5 • C min −1 ; and at the end, held for 2 min. Samples of 1 µL under split mode (split ratio 10:1) were injected. The total time taken by one run of GC was 27.50 min. Following are the other operational conditions: Ultra-pure-helium was passed over trap of sieves of molecules trapping oxygen and further utilized as a carrier gas at 40 cm s −1 of stable linear velocity. The injection port temperature was 250 • C, utilized at a ratio of 10:1 in splitless mode. The detector temperature was held at 270 • C. The instrument of hydrogen generator was installed to supply hydrogen gas to the flame photometric detector (FPD) at a constant flow rate of 69.0 mL min −1 .

Quality Control and Statistical Analysis
To ensure accuracy, standard solutions and reagent blanks were incorporated with each column. The results confirm that the glassware used in the experiment were contaminationfree; the findings of standard solutions was also satisfactory (97-99%). Each set of experiments was conducted in triplicate and the average values of the findings were documented. At various pesticide concentrations, the absorbance of adsorbents were determined by providing a standard calibration curve. For preparation and presentation of graphs, the software Origin Pro 2019 was used.  Figure 2 shows the spectra of FTIR for adsorbent AC and BCH. It was observed that each adsorbent material has a different surface functional group. Functional groups present in the surface area of adsorbent are overbearing to adsorption [47]. Peaks obtained on the spectra for AC adsorbent are 3436, 2930, 2860, 1583, and 1120 cm −1 . The documented peaks at 3436 cm −1 showed stretching vibration of the O-H bond [48,49], while those at 2930 cm −1 and 2860 cm −1 were assigned to vibration of C-H stretching bond [50].

Results and Discussion
Adsorption peak at 1583 cm −1 was noted due to vibration of C=C bond stretching in the aromatic ring, while the absorption peak at 1120 cm −1 was attributed to the C-O bond-stretching vibration [48,51]. Additionally, activated carbon FTIR spectrum has a weak adsorption peak at 873 cm −1 , which is attributed to C-H bond bending vibration in the aromatic ring replacement at a high degree level. The results showed that aromatic rings were formed due to the carbonization of AC, and in the produced aromatic ring, hydrogen contents were replaced due to 900 • C of activation temperature. The results obtained were in good agreement with the study performed by Puziy et al. [50], who studied AC FTIR spectrum synthesized from styrene-divinyl benzene at 1000 • C by activation through phosphoric acid. The presence of several coordinated carbonyl groups above the AC surface led to some sort of association [52]. Similarly, spectra of FTIR for BCH ( Figure 2b) specifies correspondence between the OH stretching and broad bands at 3425.58 [53]. The stretching at COO symmetric and COO asymmetric shows correspondence of the broad band at 1620.21 and 1404.18, respectively, while correspondence to C-O presence on the surface of BCH is indicated by the peak obtained at 1026. 12. led to some sort of association [52]. Similarly, spectra of FTIR for BCH ( Figure 2b) specifies correspondence between the OH stretching and broad bands at 3425.58 [53]. The stretching at COO symmetric and COO asymmetric shows correspondence of the broad band at 1620.21 and 1404.18, respectively, while correspondence to C-O presence on the surface of BCH is indicated by the peak obtained at 1026.12.

Scanning Electron Microscopy (SEM)
Analysis of the SEM was used to study the adsorbents' physical and morphological characteristics, as shown in Figure 3. The obtained images show chromatographic-mass pores for BCH, indicating variation in the pore size and carbon flakes during the washing step of BCH manufacturing as compared with the commercially acquired carbon. Morphologically, BCH provides a larger surface area for adsorption, which can be witnessed by comparing pre-and post-adsorption images in multiple pattern deposition, indicating

Scanning Electron Microscopy (SEM)
Analysis of the SEM was used to study the adsorbents' physical and morphological characteristics, as shown in Figure 3. The obtained images show chromatographic-mass pores for BCH, indicating variation in the pore size and carbon flakes during the washing step of BCH manufacturing as compared with the commercially acquired carbon. Morphologically, BCH provides a larger surface area for adsorption, which can be witnessed by comparing pre-and post-adsorption images in multiple pattern deposition, indicating the deposition of pesticides on BCH following the phenomenon of adsorption. The images also show that during the adsorption process, the available pores were fully occupied. Similar results were also obtained for AC following the same patterns.

X-ray Diffraction (XRD)
XRD images for AC between 22° and 25° indicate the presence of unlabeled carbon broad peaks, while the sharp peaks at 29.3° (100) and 38.9° (111) were attributed to the presence of carbon and CaO, respectively, suggesting crystallinity of the compound [54]. The peaks at 45° (200) and 65° (220) were attributed to CaO and MgO, respectively. Due to the fine alignment of layers, sharp peaks were produced, suggesting an enhanced crystalline structure. AC amorphous structure was observed due to the absence of sharp peaks in the region of 45° to 64° and represents a useful property of a good adsorbent [55,56]. Likewise, for BCH, the obtained XRD pattern expressed peaks at 2θ = 30°-40°, referring to the stacking aromatic layer structure of 2 graphite [57]. The inorganic miscellaneous compounds were indicated by the unlabeled BCH peaks between 2θ = 45°-60°. Consistency, pervasiveness, and higher contents of CaO and MgO were observed at (111), (200), and (220) peaks, respectively. At 2θ = 36°, the sturdiest and most piercing peak represents CaO and the sharpness of the peaks indicates the crystal-clear nature of the originate. The heterogeneity of BCH surface was confirmed by the peaks at X-ray diffraction ( Figure 4).

X-ray Diffraction (XRD)
XRD images for AC between 22 • and 25 • indicate the presence of unlabeled carbon broad peaks, while the sharp peaks at 29.3 • (100) and 38.9 • (111) were attributed to the presence of carbon and CaO, respectively, suggesting crystallinity of the compound [54]. The peaks at 45 • (200) and 65 • (220) were attributed to CaO and MgO, respectively. Due to the fine alignment of layers, sharp peaks were produced, suggesting an enhanced crystalline structure. AC amorphous structure was observed due to the absence of sharp peaks in the region of 45 • to 64 • and represents a useful property of a good adsorbent [55,56]. Likewise, for BCH, the obtained XRD pattern expressed peaks at 2θ = 30 • -40 • , referring to the stacking aromatic layer structure of 2 graphite [57]. The inorganic miscellaneous compounds were indicated by the unlabeled BCH peaks between 2θ = 45 • -60 • . Consistency, pervasiveness, and higher contents of CaO and MgO were observed at (111), (200), and (220) peaks, respectively. At 2θ = 36 • , the sturdiest and most piercing peak represents CaO and the sharpness of the peaks indicates the crystal-clear nature of the originate. The heterogeneity of BCH surface was confirmed by the peaks at X-ray diffraction ( Figure 4).

Column Adsorption Experiment
Absorption experiment of packed-bed column was conducted for pesticides removal using AC and BCH at various flow rates such as 0.5, 1, and 1.5 mL min −1 ; pesticides initial solution concentrations (i.e., 50 and 75 µg L −1 ); and different bed heights (10 and 15 cm), taken in adsorption glass column of a specific length of (40 cm) having 2.8 cm-diameter.

Impact of Bed Height (BH)
In adsorption column studies, breakthrough curve (BT) can be highly influenced by bed height, as pesticide treatment depends upon the used amount of packed adsorbents in the column, which subsequently describes the height of the column bed. To investigate the impact of bed height, equivalent amounts of each adsorbent of 52 g and 78 g were filled in separate columns, respectively, yielding particular bed heights of 10 cm and 15 cm, at 0.5 mL min −1 of constant flow rate, with pH of 7 and 12 µg L −1 of pesticides' aqueous solution initial concentration. Figures 5 and 6 show the adsorption of pesticides at bed heights of 10 and 15 cm, respectively. The obtained results declared that adsorption of pesticides was improved and the time of breakthrough was shifted away from the origin with the increase in bed heights. Increases in exhaust time (Cf/Ci = 1) recorded at 10 cm and 15 cm for atrazine were 3350 min to 5800 min and 3200 min to 5700 min; chlorothalanil were 3200 min to 5600 min and 3150 min to 5550 min; β-endosulfan were 3050 min to 5400 min and 2950 min to 5400 min; α-endosulfan 2900 min to 5200 min and 2850 min to 5200 min for AC and BCH, respectively. So, the maximum utilized volume for bed heights of 10 and 15 cm were 2000 mL to 3000 mL and 1800 mL to 2850 mL, for AC and BCH, respectively. At a constant flow rate, this increase in influent volume leads to longer interaction time, resulted in an increase in the ability of adsorption. So, by increasing bed height, a large volume of influent was treated, which shows that an increase in height of column bed subsequently needs a large quantity of adsorbent and, thus, provides a substantial number of binding sites for pesticides adsorption. This indicates that at 15 cm bed height, the amount of pesticides adsorbed is greater than at a bed height of 10 cm. The reason for this adsorption is that when the bed height of the column increases it creates more active and vacant sites on the surfaces of the adsorbents, creating the opportunity for longer

Column Adsorption Experiment
Absorption experiment of packed-bed column was conducted for pesticides removal using AC and BCH at various flow rates such as 0.5, 1, and 1.5 mL min −1 ; pesticides initial solution concentrations (i.e., 50 and 75 µg L −1 ); and different bed heights (10 and 15 cm), taken in adsorption glass column of a specific length of (40 cm) having 2.8 cm-diameter.

Impact of Bed Height (BH)
In adsorption column studies, breakthrough curve (BT) can be highly influenced by bed height, as pesticide treatment depends upon the used amount of packed adsorbents in the column, which subsequently describes the height of the column bed. To investigate the impact of bed height, equivalent amounts of each adsorbent of 52 g and 78 g were filled in separate columns, respectively, yielding particular bed heights of 10 cm and 15 cm, at 0.5 mL min −1 of constant flow rate, with pH of 7 and 12 µg L −1 of pesticides' aqueous solution initial concentration. Figures 5 and 6 show the adsorption of pesticides at bed heights of 10 and 15 cm, respectively. The obtained results declared that adsorption of pesticides was improved and the time of breakthrough was shifted away from the origin with the increase in bed heights. Increases in exhaust time (C f /C i = 1) recorded at 10 cm and 15 cm for atrazine were 3350 min to 5800 min and 3200 min to 5700 min; chlorothalanil were 3200 min to 5600 min and 3150 min to 5550 min; β-endosulfan were 3050 min to 5400 min and 2950 min to 5400 min; α-endosulfan 2900 min to 5200 min and 2850 min to 5200 min for AC and BCH, respectively. So, the maximum utilized volume for bed heights of 10 and 15 cm were 2000 mL to 3000 mL and 1800 mL to 2850 mL, for AC and BCH, respectively. At a constant flow rate, this increase in influent volume leads to longer interaction time, resulted in an increase in the ability of adsorption. So, by increasing bed height, a large volume of influent was treated, which shows that an increase in height of column bed subsequently needs a large quantity of adsorbent and, thus, provides a substantial number of binding sites for pesticides adsorption. This indicates that at 15 cm bed height, the amount of pesticides adsorbed is greater than at a bed height of 10 cm. The reason for this adsorption is that when the bed height of the column increases it creates more active and vacant sites on the surfaces of the adsorbents, creating the opportunity for longer contact time between adsorbate and adsorbent molecules, resulting in greater adsorption capacity. Similarly, when the bed height of the column decreased, the available adsorption vacant sites were saturated more quickly on the surfaces of the adsorbents; therefore, not enough time was attained to diffuse pesticides molecules in the pores of adsorbents. Thus, the BT curve moves to the origin and the efficacy of adsorption is reduced [41]. Relevant results were also achieved by Amiri et al. [58], who described that adsorption of pesticides and BT time increases with the rise in height of the column bed. These findings would be accredited to the enhancement in the zone of mass transfer that would adsorb the molecules additionally escaped from underlay. Consequently, the reduction resulted in the dissolution of BT curve, as an increase in mass led to specific surface area expansion, providing more vacant sites for adsorption [59]. By comparing exhaustion time for 10-and 15-cm bed heights, the results show that for a bed height of 10 cm, the exhaustion time strongly decreased, due to the phenomena of axial dispersion [60].
Water 2022, 14, x FOR PEER REVIEW 10 of 20 contact time between adsorbate and adsorbent molecules, resulting in greater adsorption capacity. Similarly, when the bed height of the column decreased, the available adsorption vacant sites were saturated more quickly on the surfaces of the adsorbents; therefore, not enough time was attained to diffuse pesticides molecules in the pores of adsorbents. Thus, the BT curve moves to the origin and the efficacy of adsorption is reduced [41]. Relevant results were also achieved by Amiri et al. [58], who described that adsorption of pesticides and BT time increases with the rise in height of the column bed. These findings would be accredited to the enhancement in the zone of mass transfer that would adsorb the molecules additionally escaped from underlay. Consequently, the reduction resulted in the dissolution of BT curve, as an increase in mass led to specific surface area expansion, providing more vacant sites for adsorption [59]. By comparing exhaustion time for 10-and 15-cm bed heights, the results show that for a bed height of 10 cm, the exhaustion time strongly decreased, due to the phenomena of axial dispersion [60].    contact time between adsorbate and adsorbent molecules, resulting in greater adsorption capacity. Similarly, when the bed height of the column decreased, the available adsorption vacant sites were saturated more quickly on the surfaces of the adsorbents; therefore, not enough time was attained to diffuse pesticides molecules in the pores of adsorbents. Thus, the BT curve moves to the origin and the efficacy of adsorption is reduced [41]. Relevant results were also achieved by Amiri et al. [58], who described that adsorption of pesticides and BT time increases with the rise in height of the column bed. These findings would be accredited to the enhancement in the zone of mass transfer that would adsorb the molecules additionally escaped from underlay. Consequently, the reduction resulted in the dissolution of BT curve, as an increase in mass led to specific surface area expansion, providing more vacant sites for adsorption [59]. By comparing exhaustion time for 10-and 15-cm bed heights, the results show that for a bed height of 10 cm, the exhaustion time strongly decreased, due to the phenomena of axial dispersion [60].

Physical Properties of AC and BCH
Significant physical properties of BCH and AC include bulk density, porosity, surface area, particle size, and water holding capacity. BCH showed a lower density of 0.42 g cm −3 than AC having 34.4 g cm −3 bulk density at particle size of 250 µm. The pore volume of AC was 1.39 nm while that of BCH was 0.03-0.02 nm. Similarly, water holding capacity of BCH was greater than that of AC, while solid density of AC was greater than that of BCH. Both the adsorbents had high surface area, resulting in good water holding capacity, as shown in Table 1.

Impact of Initial Concentration (Ci)
Breakthrough curves for packed columns of both AC and BCH adsorbents at 50 µg L −1 and 75 µg L −1 of inlet concentrations of pesticides are shown in Figures 7 and 8, respectively, while all other conditions such as flowrate rate (0.5 mL min −1 ), influent pH 7, and height of bed (5 cm) were kept constant. Breakthrough time shows a decrease for both AC and BCH adsorbents when the initial concentration of the pesticides increases, because the sites of adsorbent are exhausted rapidly with higher concentration [41]. Similar results were also obtained by Pradhan et al. [6], who reported that the increase in inlet concentration resulted in the decrease in adsorption rate of pesticides. This suggests that the adsorbent-available binding sites were rapidly occupied with pesticide molecules at greater concentration, resulting in earlier saturation of adsorbent and the time of exhaustion being reached earlier [61]. The result indicates that when influent pesticides solution concentration increases from 50 to 75 µg L −1 , exhaustion time decreases for atrazine from 520 min to 390 min and 480 min to 360 min, chlorothalanil from 480 min to 360 min and 440 min to 330 min, β-endosulfan from 440 min to 330 min and 400 min to 300 min, and α-endosulfan from 400 min to 300 min and 360 min to 270 min on AC and BCH, respectively, due to the rapid saturation of the adsorbent sites. This is due to the fact that at lower influent pesticides solution concentrations, a decrease in diffusion coefficient and mass transfer driving force leads to the adsorbate molecules' good diffusion in the adsorbent pores. Consequently, increases in the contact time were reported and the solution left the column in a longer time. Hence, at lower concentration, the ability of adsorbent adsorption increased. However, in the column driving forces for diffusion of pesticides molecules were boosted in the higher inlet concentration. Further, during the process of adsorption, the influent increasingly occupied and therefore rapidly saturated the active sites of the adsorbent, resulted in the decreased extent of adsorptions [62,63]. Relevant results were obtained by Raiman et al. [8] who investigated atrazine adsorption in a fixed-bed column from prepared aqueous solution. The obtained results showed that atrazine adsorption decreases due to the rise in initial concentrations of atrazine in synthesized aqueous solution (used as an influent). Similarly, Bayat et al. [59] suggested that the adsorption sites rapid saturation can be the cause of high inlet concentration, resulting in accelerated breakthrough and reaching the saturation point in less time. In summation, from our findings, it can be inferred that adsorption can be significantly affected by the influent initial concentrations in a fixed-bed column, thus, effecting the morphology, molecule charge, and adsorbent surface properties.

Impact of Flow Rate (Q)
In adsorption studies, flow rate affects the breakthrough curve, predicts the contact time of the influents with adsorbent, and evaluates the capacity of adsorbent uptake of the column. Flow rate's impact on pesticides combined solution adsorption onto AC and BCH was investigated by varying the flow rate to 0.5, 1, and 1.5 mL min −1 with 12 µg L −1 of initial concentration, bed height of 5 cm, and neutral pH of 7. The obtained curves at 0.5, 1, and 1.5 mL minˉ¹ flow rates are shown in Figures 9-11, respectively. The obtained

Impact of Flow Rate (Q)
In adsorption studies, flow rate affects the breakthrough curve, predicts the contact time of the influents with adsorbent, and evaluates the capacity of adsorbent uptake of the column. Flow rate's impact on pesticides combined solution adsorption onto AC and BCH was investigated by varying the flow rate to 0.5, 1, and 1.5 mL min −1 with 12 µg L −1 of initial concentration, bed height of 5 cm, and neutral pH of 7. The obtained curves at 0.5, 1, and 1.5 mL minˉ¹ flow rates are shown in Figures 9-11, respectively. The obtained

Impact of Flow Rate (Q)
In adsorption studies, flow rate affects the breakthrough curve, predicts the contact time of the influents with adsorbent, and evaluates the capacity of adsorbent uptake of the column. Flow rate's impact on pesticides combined solution adsorption onto AC and BCH was investigated by varying the flow rate to 0.5, 1, and 1.5 mL min −1 with 12 µg L −1 of initial concentration, bed height of 5 cm, and neutral pH of 7. The obtained curves at 0.5, 1, and 1.5 mL min −1 flow rates are shown in Figures 9-11, respectively. The obtained results showed that, at lower flow rate, the exhaust time and breakthrough increased, suggesting the maximum utilization of the adsorbents AC and BCH for pesticides adsorption; at high flow rate, breakthrough and exhaust time decreased. The decreases in exhaust time for atrazine were 1750 min to 600 min and 1700 to 570 min, chlorothalanil 1680 min to 570 min and 1640 min to 540 min, β-endosulfan 1620 min to 510 min and 1590 min to 480 min, and α-endosulfan 1560 min to 480 min and 1530 min to 420 min at flow rates ranging from 0.5 to 1.5 mL min −1 on AC and BCH, respectively. This indicates that at 0.5 mL min −1 of lower influent flow rate, the adsorbent shows higher adsorption capability. Similar results were also obtained by Raiman et al. [8], who reported that with the increase in flow rate, decreased in the adsorption of pesticides were noted. The reason for this aggravated capability of adsorption is that the increase in mass transfer into the adsorbent pores occurs due to the increase in the time of residence; consequently, on the surface of adsorbent, the pesticides' molecules gain greater access to approach active binding sites. Subsequently, uptake of pesticides increases. Although, when the flow rate increased, a decrease in the breakthrough time and exhaust time was reported due to the shorter mass transfer zone; therefore, the adsorption of pesticides was lower because of minimum contact time amongst pesticides molecules and adsorbent [41]. Similarly, Amiri et al. [62] studied that at higher breakthrough times and lower flow rates, more accessible adsorption sites were available and molecules of pesticides adsorb easily, so the adsorption quantity decreased with increasing flow rate. Relevant results were also obtained by Xu et al. [63]. According to him, higher driving forces were produced at higher influent flow rate in the column for mass transport, which ultimately reduce the contact time; therefore, no sufficient time for pesticides molecule diffusion into the adsorbent pores was available. Bayat et al. [59] also reported that fixed-bed column reaches an early saturation point due to high influent flow rate. This is why, before leaving the column, less of the solution volume is purified and the capacity of adsorption decreases. results showed that, at lower flow rate, the exhaust time and breakthrough increased, suggesting the maximum utilization of the adsorbents AC and BCH for pesticides adsorption; at high flow rate, breakthrough and exhaust time decreased. The decreases in exhaust time for atrazine were 1750 min to 600 min and 1700 to 570 min, chlorothalanil 1680 min to 570 min and 1640 min to 540 min, β-endosulfan 1620 min to 510 min and 1590 min to 480 min, and α-endosulfan 1560 min to 480 min and 1530 min to 420 min at flow rates ranging from 0.5 to 1.5 mL minˉ¹ on AC and BCH, respectively. This indicates that at 0.5 mL min −1 of lower influent flow rate, the adsorbent shows higher adsorption capability. Similar results were also obtained by Raiman et al. [8], who reported that with the increase in flow rate, decreased in the adsorption of pesticides were noted. The reason for this aggravated capability of adsorption is that the increase in mass transfer into the adsorbent pores occurs due to the increase in the time of residence; consequently, on the surface of adsorbent, the pesticides' molecules gain greater access to approach active binding sites. Subsequently, uptake of pesticides increases. Although, when the flow rate increased, a decrease in the breakthrough time and exhaust time was reported due to the shorter mass transfer zone; therefore, the adsorption of pesticides was lower because of minimum contact time amongst pesticides molecules and adsorbent [41]. Similarly, Amiri et al. [62] studied that at higher breakthrough times and lower flow rates, more accessible adsorption sites were available and molecules of pesticides adsorb easily, so the adsorption quantity decreased with increasing flow rate. Relevant results were also obtained by Xu et al. [63]. According to him, higher driving forces were produced at higher influent flow rate in the column for mass transport, which ultimately reduce the contact time; therefore, no sufficient time for pesticides molecule diffusion into the adsorbent pores was available.
Bayat et al. [59] also reported that fixed-bed column reaches an early saturation point due to high influent flow rate. This is why, before leaving the column, less of the solution volume is purified and the capacity of adsorption decreases.

Thomas Model
In a fixed-bed column system, to describe the dynamic adsorptions of different pollutants, the popular Thomas equation has been used broadly to observe BTC [64]. By applying nonlinear regression analysis, the experimental data obtained were best fitted to Thomas' model. The model accuracy was evaluated on the basis of determined coefficient (R 2 ) calculations. The results indicate that Thomas' model satisfactorily describes experimental data at each operating condition and fit the breakthrough curves well, and due to higher R 2 (0.9986) value, nearly a perfect match amongst the estimated and experimental data was accomplished. Values of Thomas' constants (kTH) and adsorption (q 0 ) were also used to describe the dynamic adsorption behavior of AC and BCH, for pesticides adsorption under several operational parameters. With the increase in flow rate from 0.5 to 1.5 mL min −1 , the k TH value of all selected pesticides increases for both AC and BCH. Similar trends were also obtained for the values of q o for both the adsorbents, as presented in Table 2. The results obtained are in good agreement with the study performed by Odunola et al. [65]. The values of R 2 at 0.5 mL min −1 of flow rate for atrazine were 0.9427 and 0.9637; chlorothalanil, 0.9588 and 0.9628; β-endosulfan, 0.9353 and 0.9389; α-endosulfan, 0.9583 and 0.9389 for AC and BCH, respectively, which shows good fit to the adsorption data. Baharami et al. [41] obtained the same results by studying the adsorptions of 2, 4 D pesticides onto the adsorbents "AC and BCH" and the obtained data were examined using Thomas' model, which shows best fit to the adsorptions data. Yoon-Nelson's model is a general mathematics model investigating 50% of the breakthrough time. Basically, the model measure, proportionality "rate of decrease in the probability of adsorption for each adsorbate molecule", and "the probability of adsorbate adsorption and the probability of adsorbate breakthrough on the adsorbent" [65]. Ln cf/ci-cf against time t linear plot were elucidated by Yoon-Nelson model, presented in Table 3. The value of Kyn for both AC and BCH increases with the rise in the flow rate. The Kyn value was observed in the range of 0.001 and 0.0066 mg g −1 for AC and 0.0019 and 0.0086 for BCH. The τ value for AC and BCH was found to be between 0.001181-930.6111 and 217.668-1066.368 mL min −1 mg −1 , respectively. Relevant results was also given by Bayat et al. [59], who studied diazinon removal through fixed-bed column. According to higher R 2 values, the fluent removal of pesticides was well-described by Yoon-Nelson's model under optimal conditions onto AC and BCH, which illustrate the model's validity for this study. A comparison of the obtained results with literature data is summarized in Table 4.

Conclusions
This study demonstrates that pesticides adsorption from aqueous solutions in a fixedbed column system might be potentially useful. As an adsorbent, both AC and BCH show high adsorption affinity for selected pesticides. Bed height (BH), flow rate (Q), and influent initial concentration (Ci) were the essential parameters used in the study. The results reveal that pesticides adsorption increases with the rise in column bed height from 5 cm to 15 cm, while a decrease in adsorption was found when flow rate increases from 0.5 mL min −1 to 1.5 mL min −1 , and influent initial concentration from 50 µg L −1 to 75 µg L −1 . Such promising results provide a basis for implementation of a novel continuous treatment system for water contaminated with pesticides. Thomas' and Yoon-Nelson's models welldescribe the dynamic adsorption behavior of a fixed-bed column system under optimal conditions (R 2 = 0.9427 and R 2 = 0.9921), respectively. The studied adsorption technique was suitable for each environmental condition and, for adsorbents preparation, rely on available resources, which confirm its cost-effectiveness. The outcomes of the current study determine that under optimal conditions both the adsorbents could be efficiently implied as best adsorbents to adsorb pesticides from prepared aqueous solutions.