Adsorption properties of sugarcane bagasse and corn cob for the sulfamethoxazole removal in a fixed-bed column

Natural adsorbents are a good alternative to remove antibiotic residues from wastewater. In this study, the adsorption capacity of sulfamethoxazole (SMX) onto sugarcane bagasse (SB) and corn cob (CC) in a continuous fixed-bed was compared. Brunauer Emmett Teller, Fourier transform infrared (FTIR), Boehm titration, and point of zero charge (pHpzc) were used to characterize both adsorbents. The adsorption capacity (qe) and the removal percentage of SMX (% R) were investigated at different different flow rates (2, 5, and 7 mL min− 1) and adsorbent masses (4 and 6.4 g), and a constant initial concentration of 5 mg L− 1. The results of the characterization showed that SB has a morphology with more dispersed particles and a specific surface higher than CC (2.6 > 1.2 m2 g− 1). Boehm titration indicates that both the surface of SB and CC have a greater amount of acid groups, which is in agreement with FTIR and pHpzc results. The continuous fixed-bed experiments showed that % R and qe of SMX are higher with SB in all the tests. The highest qe and maximum % R was 0.24 mg g− 1 and 74% with SB, and 0.15 mg g− 1 and 65% using CC. In most cases, the qe of both adsorbents decreased with the increase of flow rate and bed height. An analysis suggests that hydrogen bonds could be the main factor favoring the SMX adsorption with SB. Finally, the intraparticle diffusion was the rate-controlling step, predominating the pore-volume diffusion resistance.


Introduction
Antibiotics are widely used in humans and animals to fight diseases caused by bacteria. In animals, they have also been used to a great extent to promote their growth and for the prophylaxis of diseases. After administration, they are partially metabolized, and a significant portion of the antibiotic can be excreted in the urine or feces as the parent compound or in conjugated forms. In fact, it has been estimated that between 70 and 90% of antibiotics administered in animals are excreted through urine and feces [1]. As a result, these residues of antibiotics and their metabolites are released into the environment.
Residual antibiotics for human and animal use can enter the environment through several pathways, including domestic and hospital wastewaters discharge, leaching, and runoff from land to which animal wastes with antibiotics have been applied [2]. Sulfamethoxazole (SMX) is a bacteriostatic antibiotic, and it is commonly used to treat urinary tract infections, sinusitis, and toxoplasmosis. After being ingested, SMX and its main metabolite, N 4 -acetyl-sulfamethoxazole (Ac-SMX), are excreted in the urine. In human metabolism, SMX and Ac-SMX are excreted in approximately 15-25 and 50% of the administered dose, respectively [3]. However, in animal metabolism, approximately 70% is excreted as the parent compound, and 28% as Ac-SMX [4]. SMX and Ac-SMX have been found in domestic and hospital wastewaters. Normally, their concentration varies in the range of ng L − 1 and μg L − 1 . In Canada, SMX was the most concentrated antibiotic in effluents of a wastewater treatment plant (WTP) with 3.28 μg L − 1 [5]. Similarly, in China SMX and Ac-SMX were detected in WTP influents in the concentration range between 13.5-152 and 83-299 ng L − 1 , respectively, while in the effluents their concentrations were reduced to 11.4-145 and 89-208 ng L − 1 , respectively [6].
Multiple studies have shown that the conventional WTPs are ineffective in completely removing antibiotic residues, with a removal percentage for SMX only between 20 to 90% [7]; and in some cases, even a negative removal efficiency has been reported [8]. Due to the ineffectiveness of WTPs to eliminate SMX, this antibiotic has currently been found in surface waters, groundwater, and even in drinking water [9]. For instance, in freshwaters from Africa and Germania SMX was found in concentrations of up to 53.8 μg L − 1 and 100 ng L − 1 , respectively [10,11]. In North Carolina, SMX was found at values lower than 10 ng L − 1 [12]. Similarly in Ecuador, SMX reached drinking water at a concentration lower than 20 ng L − 1 [13]. Although the levels of SMX found in surface and drinking water are not high enough to affect human and animal health, due to the frequent, extensive, and uninterrupted use of these types of drugs, these very low concentrations could pose a threat to the development of antibiotic resistant bacteria.
Adsorption is an effective and appropriate technology to remove antibiotic residues present in wastewaters at very low concentrations. Many adsorbents have been studied to remove SMX such as granular activated carbon, lignite activated coke, microporous organic polymers, graphene nanocomposite, metal-organic frameworks, biochar, and other carbon-based materials with high adsorption capacity (> 100 mg g − 1 ) [14,15], and they could be ideal for pilot and industrial applications. However, the methods of obtaining these adsorbents are expensive, so their large-scale application is economically unfeasible. For this reason, scientists have intensified the development and search for low-cost adsorbents. Materials like agricultural waste, industrial byproducts, and natural materials with little processing can be used as adsorbents for the removal of antibiotics. All these materials have good properties and have the advantage in that their production cost is very low. Some of the raw materials that have been used for SMX removal in batch are spent mushroom substrate, corn cob (CC), peanut shell, walnut shell, agricultural soil, and sugarcane bagasse (SB) [16,17].
CC and SB are two lignocellulosic residues with high potential to be used as adsorbents in Ecuador due to their large production and availability. In Ecuador, for every kg of corn harvested, 0.186 kg of CC are produced [18]. Similarly, 1 kg of SB is obtained for every 3.5 kg of sugar cane processed [19]. In the literature consulted there are few studies that use SB and CC in their natural state for the removal of pharmaceutical compounds. SB and CC have shown good adsorption properties for the removal of ciprofloxacin, acetaminophen, and tetracycline [20,21], with an adsorption capacity greater than 5 mg g − 1 in batch studies. However, their efficacy in removing SMX and other antibiotics in a fixed-bed column has not yet been studied.
In this study, the adsorption properties of two lowcost adsorbents, SB and CC, for removing SMX from synthetic solutions were investigated. Knowing their potential as adsorbents to remove antibiotics is our prime aim. With this information, we will know which of these adsorbents has a better practical utility and could be used for further studies to improve even more its adsorption properties with methods such as surface modification, production of composites, among other approaches. The adsorption studies were carried out in a lab-scale fixed-bed column, and the effect of the bed height and flow rate was investigated. Besides, the transport parameters were estimated to elucidate the ratelimiting step in the SMX adsorption.

Materials and methods
Reagents SMX with a purity of 99% supplied by Sigma-Aldrich was used in this study. Methanol of analytical grade Merck with a purity of 99% was used to dissolve SMX. The SMX solutions were prepared with distilled water and with 1% v/v methanol. All synthetic solutions had a concentration of 5 mg L − 1 of SMX. The pH of the solution was adjusted to 6 with addition of 0.1 N HCl solution. The initial and residual concentrations of SMX were determined by the Visible Genesys 10S UV spectrophotometry technique from Thermo SCIENTIFIC, at a wavelength of 261 nm. The physicochemical properties of SMX are detailed in Table 1.

Adsorbents' preparation and characterization
Raw SB and CC were obtained from a sugar mill and a local farm, in Azuay, Ecuador. Before their use in adsorption tests, SB and CC were washed repeatedly with distilled water in order to remove impurities and residual sugars. Then, these were dried in an oven at 60°C for 8 h. Finally, the size of the fibers was reduced using a hammer mill and subsequent sieving. The fraction with a particle diameter between 0.84 and 0.42 mm was characterized and eventually used in the adsorption tests.
As physical properties, the specific surface area was estimated using Brunauer Emmett Teller method by nitrogen physisorption using an ASAP 2020 Micromeritic instrument; the bulk density, particle density, and the bed porosity were also estimated with the methodology described in our previous study [22]. Regarding chemical properties, the amount of surface acidic and basic groups of both adsorbents were quantified by the acidbase titration method. The point of zero charge (pH PZC ) was determined by the potentiometric curves, and the functional groups of SB and CC were identified with FTIR spectroscopy. The spectra were obtained using a HATR attenuated total reflectance accessory, with a ZnSe crystal and a resolution of 4 cm − 1 and 100 scans in the range of 4000 and 1300 cm − 1 .

Continuous fixed-bed experiments
A glass column 35 cm in height and 2.2 cm in internal diameter was used for the adsorption tests. For the experimental setup of the column, the adsorbent previously weighed was introduced into the inside the column, and 1 cm of gravel of 2 mm diameter was placed at the bottom and the top of the fixed-bed to prevent the adsorbent from being entrained by the solution and to avoid the floating of the bed and provide a better distribution of the solution. The SMX solution was pumped into the bed by a peristaltic pump with downward flow and the samples were collected in the outlet of the column until the adsorbent was saturated.
Six studies were carried out with each adsorbent. The effect of flow rate Q (at 2, 5, and 7 mL min − 1 ) and bed height H (two heights corresponding to an adsorbent mass of 4 and 6.4 g) on the breakthrough curve was studied as can been seen in Table 2. To compare the adsorption properties of the adsorbents, the same mass was used for each adsorbent (m) in each test.

Column performance analysis
The performance column in each test was investigated with eight parameters that describe the operation of the fixed-bed column. The breakthrough time (t b ) and saturation time (t s ) were estimated when the SMX concentration at the column outlet reaches 5% (C/C i = 0.05) and 75% (C/C i = 0.75) of the initial concentration, respectively. The volume of the SMX solution treated until the saturation time was estimated using Eq. (1).
The total amount of SMX removed q total (mg) is represented by the area under the breakthrough curve, and it was obtained by Eq. (2). The total amount of SMX passing through the adsorbent bed until saturation time m total (mg) was calculated using Eq. (3). When the adsorption column reaches equilibrium, the adsorption capacity q e (mg g − 1 ) can be determined by Eq. (4).
where C R is the concentration of SMX adsorbed (mg L − 1 ), and C i is the initial concentration of SMX (mg L − 1 ). Additionally, the total percentage of antibiotic removed % R was obtained from Eq. (5). Finally, the length of the unused bed LUB (cm) was calculated using Eq. .
Transport parameters To better understand which mechanism is the ratelimiting step in the SMX adsorption, the following transport parameters were estimated: film or external diffusion coefficient k f , surface diffusion coefficient D s , and pore volume diffusion coefficient D p . The empirical correlations used are shown in Eqs. (7), (8), and (9) [21,23].
where D m is the molecular diffusivity of SMX (m 2 s − 1 ), d p is the particle diameter of the adsorbent (m), v is the superficial velocity of the SMX solution (m s − 1 ), ρ (kg m − 3 ) and μ (kg m − 1 s − 1 ) are the density and the dynamic viscosity of the SMX solution, r p (m) and ɛ p are the radius and porosity of the adsorbent particle (Table 3), and τ is the tortuosity factor of the adsorbent. D m and τ were estimated using Eqs. (10) and (11) [24].
where α is a solvent association parameter, M (g mol − 1 ) is the molecular weight of the solvent, and V m (cm 3 mol − 1 ) is the molar volume of SMX at its normal boiling point (see Table 1). Since the intraparticle diffusion involves both surface and pore diffusion, both mechanisms can be represented by an effective intraparticle diffusion coefficient (D e ), Eq. (12) [23].
where ρ b is the bed porosity (kg m − 3 ), and f ′ (C) is an average value of dq/dC from an isotherm. The f ′ (C) was 0.029 L g − 1 according our previous studies.

Results and discussion
Characterization of adsorbents Physical properties The obtained physical properties of SB and CC are shown in Table 3. The particle and bulk density of CC is greater than that of SB, hence the bed height with CC is higher than with SB with the same amount of biosorbent (as can be seen in Table 2). Similarly, the bed porosity with CC was higher than with SB, which means there is more space between the particles for the ACT solution to come into contact with CC. On the contrary, the value of the specific surface area of SB is twice the value of CC with the same particle size.

Chemical properties
Figures 1a and b show the determination of the point of zero charge, and was 6.1 and 5.5 for SB and CC, respectively; which means that at this pH value, the total net charge on the surface of SB and CC is zero. Penafiel et al. [17] reported a pHpzc value of 5.9 for SB from Ecuador; this indicates that the pHpzc for this biosorbent is around 6, which means that SB has almost null surface charge at pH of SMX solutions. The pH pzc values also mean that both SB and CC have a slightly acid character. These results are in accordance with those reported by Vera et al. [22]. Figures 1c and d show the Boehm titration curves for SB and CC, respectively, and Table 4 shows the value and percentage of acid and basic groups. The results indicate that both SB and CC have a greater amount of acid functional groups rather than basic groups. These results are in agreement with those obtained for pH PZC . The acid character of the surface of SB and CC shows that the carboxyl (−COOH), lactone (−OOR), and phenolic hydroxy (−OH) groups are predominantly present on their surface [25]. Furthermore, a greater quantity of acidic sites translates into a greater presence of oxygenated functional groups, and this has been shown to increase the adsorption capacity in activated carbons and chemically modified natural adsorbents [26]. For this reason, SB and CC could be potential adsorbents for SMX removal. The FTIR analysis supported the Boehm titration results. Figure 2a and b show the infrared spectra of SMX, SB, CC, SB-SMX, and CC-SMX. An intense peak at 3336 cm − 1 shows O-H stretching of phenolic hydroxyl or carboxyl groups of SB and CC. The peak at 1724 cm − 1 corresponds to C=O stretching of carboxyl and lactone groups [27]. Also, the peak at around 1371-1374 cm − 1 is assigned to C-O groups of carboxylic acid, alcoholic, and phenolic groups. Other major functional groups present are C-H of aliphatic groups around 2888-2896 cm − 1 ; C-O of ester and ether groups at 1034-1038 cm − 1 ; stretching vibration of C=C of aromatic rings at 1603 cm − 1 , and C-O-C and C-O at 1238-1245 cm − 1 attributed to the bending of CH 3 groups of cellulose and hemicellulose of SB and CC. After adsorption, some peaks are observed around 1400-1620 cm − 1 attributed to -N-H groups corresponding to SMX [28]. Additionally, for the spectra of CC, the intensity of the absorption peaks at 3336 and 2888 cm − 1 changed slightly to compare to CC-SMX spectra. Similarly, this happened for the spectra of SB and SB-SMX at the same peaks with a change more significant. This indicates that the SMX adsorption on SB and CC occurs mainly on O-H, C-H, and C-O bonds, where hydrogen bonds are the most important interactions [29].

Continuous fixed-bed experiments Effect of flow rate
The effect of flow rate on the breakthrough curve was studied at 2, 5, and 7 mL min − 1 , at bed heights at 15 and 25 cm, and at an initial concentration of 5 mg L − 1 . The results obtained with SB and CC are observed in Fig. 3. As evidenced in Fig. 3a and b, the breakthrough and saturation times increase as the flow rate decreases, this happens at 15 and 25 cm. Thus, the breakthrough and saturation times are greater at lower flow rates (Table 5), which translates into more antibiotic adsorbed. While high flow rates tend to drive turbulence within the interstitial spaces of the bed, and this turbulence increases the possibility of axial dispersion effects occurring, limiting the diffusion of SMX into the pores of SB; this turbulence may be a cause for lower breakthrough and saturation times. Furthermore, the lower the flow rate, the longer the residence time of the SMX in the column, which means that there is a greater opportunity for SMX to reach the macropores of the adsorbent at low flow rates. This may be the main reason why q total decreases as the flow rate increases, as shown in Table 5. Furthermore, if the residence time of the SMX in the bed column is not long enough, the adsorption equilibrium is not reached within the column, since the solution with SMX leaves the column before it occurs [30]. Figure 3c and d show the influence of flow rate when corn cob is used. As with the SB, the adsorbent bed reaches saturation faster at high flow rates. In fact, when working at 7 mL min − 1 and 7 cm, the SMX concentration at the outlet of the column reaches half of the inlet concentration (C/C i = 0.5) only 5 min after starting the operation. In the same way, it occurs at 7 mL min − 1 and 11 cm of bed height. This shows the low affinity of SMX for CC when operating at high flow rates. A singularity that can be noticed is that the curves have a particular shape since in the initial region the curve is almost a straight line, then they present high slopes in the transitory region, and then decrease as they progress towards full saturation. Furthermore, the breakthrough curves do not present the sigmoidal tendency, which is generally observed in ideal adsorbate-adsorbent systems, with a favorable adsorbate removal; however, this tendency was not observed neither in the SMX-CC nor in SMX-SB. The high slopes in the curves reveal that the mass transfer is not controlled by diffusion, giving rise to the possibility of an instantaneous equilibrium between the liquid phase and the phase adsorbed. Figure 4a shows the influence of the bed height for SB; the breakthrough curves were obtained at 15 and 25 cm, and with a flow rate of 2 mL min − 1 . An increase in H significantly prolongs the breakthrough and saturation time. For example, t s increases from 75.96 to 141.82 min when changing from 15 to 25 cm ( Table 5). The increase in H causes a greater quantity of adsorbent material, which means a greater surface area and therefore a greater quantity of active sites. Furthermore, with a higher bed height, the time it takes for the antibiotic solution to travel through the column is longer, which increases the contact time between the SMX and the active sites of the adsorbent.

Effect of bed height
The effect produced by the variation of H in breakthrough curves is less significant with CC (Fig. 4b). Contrary to what happened with SB, the breakthrough times practically coincide at both heights, for all the flow rates ( Table 6). In effect, the curves overlap in the initial region, but as time passes, they begin to differ; hence the saturation times are different. The increase in H from 7 to 11 cm results in a doubling t s ; for instance, it varied from 77.9 min to 168.2 min with a flow rate of 2 mL min − 1 ( Table 6). This effect may be due to the behavior of the fluid inside the column. At low bed heights, the effects of axial dispersion can be considerable and predominant in mass transfer phenomena, which leads to a difficult and slow diffusion of the SMX from the liquid to the solid phase. But at higher bed heights, the axial dispersion becomes negligible. Table 5 shows the fixed-bed parameters when the column is packed with SB. The parameters V and m total increase as Q and H increase. For instance, the increase in flow rate from 2 to 7 mL min − 1 allows an increase in m total of 0.74 mg when working at a bed height of 15 cm. On the contrary, with high flow rates q total decreased, but it increases with the increase in H. In the case of the adsorption capacity, it is inversely proportional to the feed flow rate, but no particular trend was observed with bed height. However, q e and q total values are higher at a flow rate of 2 mL min − 1 and 25 cm of bed height. Similarly, the maximum % R was 74%, at the same operating conditions. This occurs since there is a greater number of active sites available and a longer contact time between SMX and SB at higher bed heights and lower flow rates. When the column is packed with CC, the performance parameters have the same behavior as with SB ( Table 6).

Performance parameters of the adsorption column
The maximum values of V and m total are presented at the highest H and Q. In contrast, % R is very favorable at the lowest flow rate and bed height. Additionally, the maximum q total and q e were favored at 2 mL min − 1 and 11 cm of bed height. The main reason why q e decreases with increasing the flow rate may be due to the reduced contact time between the SMX solution and the pores of adsorbents. In this way, at high flow rates, all adsorbent active sites are not accessible and are not fully occupied for SMX. These results are in agreement with other studies on the removal of antibiotics [31,32]. The q e also decreases with increasing H due to the overlap of active sites with the increase in adsorbent mass or bed height, indicating that not all these sites are accessible by the SMX molecule. Similarly, channeling effects and poor solution distribution may be other factors in this effect [33]. Similar behavior has been reported by Gupta and Garg [31] in the ciprofloxacin removal using activated carbon, and Saadi et al. [32] in the azithromycin adsorption by modified clinoptilolite.

Comparison of SB and CC
In order to establish which adsorbent has better properties for the SMX removal, the breakthrough curves obtained under the same operating conditions were compared. Figure 5a shows the curves of SB and CC resulting at 2 and 5 mL min − 1 , with an adsorbent mass of 6 g. The curves with SB are much longer in time than those with CC, and therefore, the area above the breakthrough curves is greater when using SB. This shows that the SMX has a higher affinity for the active sites of SB rather than CC. For this reason, % R and q e were higher with SB in all the tests carried out (Fig. 5b). In certain cases, q e triples when SB is used versus CC; as it is the case of the test at 7 mL min − 1 and 6 g, in which q e was 0.20 mg g − 1 with SB and only 0.067 mg g − 1 with CC. The maximum q e for SB and CC obtained was 0.24 and 0.15 mg g − 1 , respectively. Additionally, the adsorption   Tables 5 and 6. These results indicate that CC has higher adsorption capacity per surface than CC in almost all adsorption tests. The maximum q e,s for SB and CC was 0.091, and 0.12 mg s − 2 , respectively. This fact is mainly attributed to the low specific surface area of CC. Similar results were obtained by Penafiel et al. [17], where SB had higher adsorption capacity per surface than activated carbon; nonetheless the activated carbon had an adsorption capacity 10 times higher than SB to remove ciprofloxacin. The fact that SB has better adsorption properties against CC can be mainly attributed to its higher specific surface, which means a greater number of active sites available for the SMX adsorption. Also, the chemical properties of SB can promote better adsorption of SMX. SB has a slightly higher amount of acid groups than CC (Table 4), this implies more carboxyl, lactone, and phenolic hydroxy functional groups, resulting in a higher adsorption capacity [26].
Additionally, SMX has two pK a values (Table 1), pK a1 = 1.7 corresponds to the protonation of the amino group (−NH 2 ), while pK a2 = 5.7 corresponds to the deprotonation of the amide group (−NH-) ( Fig. 6a and Table 1). SMX will be predominantly positively charged if pH < pK a1 (SMX + ), as a neutral species if pK a1 < pH < pK a2 (SMX 0 ), and negatively charged if pH > pK a2 (SMX − ) [34]. Similarly, according to the pH PZC of SB and CC, at pH of 6 SB has a neutral global charge on its surface, and CC surface is negatively charged. This condition causes electrostatic repulsions between SMX − and CC with a decrease in the adsorption of the SMX, and there were no electrostatic interactions between SMX − and SB.
Furthermore, the formation of hydrogen bonds and hydrophobic interactions have been reported as predominant mechanisms in the adsorption of SMX using activated carbon, clays, and resins [35]. Most of the time, hydrogen bonds were formed between -NH 2 or SO 2 N-groups of SMX with the carbonyl (−COOH), hydroxyl (−OH), and primary amide (−NH 2 ) functional groups of the adsorbent. As the functional groups -COOH and -OH are mostly present in SB and CC, the possibility of hydrogen bonding as a dominant mechanism in SMX adsorption is not ruled out (Fig. 6b). Finally, the adsorption capacity and removal percentage of CC and SB were compared with other biosorbents, which were used to remove antibiotics as detailed in Table 7.
As can be seen, the adsorption properties for SB and CC are in the same range as other biosorbents. SB and CC had adsorption capacities higher than fish waste to remove SMX, but lower than rice husk and cork.

Transport parameters
The transport process during SMX adsorption into SB was analyzed. This process involves four steps: bulk transport by diffusion and convection, film diffusion, intraparticle diffusion, and adsorptiondesorption reaction (Fig. 7). It is well known that the second and third stages occur slowly, and either could be the rate-limiting step in the adsorption process. The tortuosity factor for SB was 15.3, which is agreement with the value reported by Pauletto et al. [24]; the high tortuosity is due to the fact that the pore geometry of sugarcane bagasse is more disordered and chaotic compared commercial adsorbents such as activated carbon [24]. The estimated values of D s , D p , and k f are presented in Table 8; as can be seen, both D s and D p are not affected by changes in operation conditions, and were 3.86 × 10 − 12 and 9.89 × 10 − 12 m 2 s − 1 , respectively; which are in the range reported for other agro-waste adsorbents [24], which indicates that the pore and surface diffusion present high resistance in the transport processes. On the other hand, k f increases with the change in flow rate, this is because the thickness of the liquid film decreases as the flow rate increases [23]. Similarly, to D s and D p , D e did not change with Q and H, and it was 6.68 × 10 − 12 m 2 s − 1 . Finally, the ratelimiting step was established with the Biot number (Bi), which measures the relative rate between film diffusion and intraparticle diffusion.
According to Pauletto et al. [24], if Bi < 0.5 the film or external diffusion is the rate-limiting step, while if Bi > 30, the intraparticle diffusion predominates and controls the adsorption. In this study, Bi numbers for all test are larger than 30, indicating that intraparticle diffusion is the rate controlling step for the SMX adsorption on SB. Additionally, it was observed that Bi number increases with the flow rate, which means that the film diffusion resistance decreases and the interparticle diffusion is more relevant as the flow rate increases. It is well known that the surface diffusion is predominant in adsorbents with high content of micropores; however, our previous work has shown that the pore distribution of SB is more dispersed with predominant larger pores (macropores and mesopores) [17]. Therefore, it can be inferred that the pore diffusion has a higher contribution in the intraparticle diffusion.

Conclusions
This study characterized and evaluated the adsorption properties of SB and CC to remove SMX from synthetic solutions in a fixed-bed column. The main conclusions about the adsorbents' characterization are that SB had a specific surface area twice that of CC. The point of zero charge was 6.1 for SB and 5.5 for CC; which indicates a slightly acid character. This was corroborated with the Boehm titration results where the functional acid groups were higher than 80% for both adsorbents; this acid character was mainly due to the presence of carboxylic acid, alcoholic, and phenolic groups. In most fixed-bed experiments, the adsorption capacity of both adsorbents decreased with increasing flow rate and bed height, and the maximum adsorption capacity was 0.24 and 0.15 mg g − 1 for SB, and CC, respectively. This indicates that the SMX molecule has a higher affinity for the active sites of SB than for CC. The main factors that explain the better adsorption capacity of SB were a greater surface area, electrostatic attractions, and the formation of hydrogen bonds between SB and SMX. Besides, it was observed that the SMX adsorption was controlled by the intraparticle diffusion, which was more relevant as flow rate increased. Sugarcane has the potential to be used in wastewaters treatment and could be used to extend the study with chemical modifications.