Removal of Malachite Green Using Hydrochar from PALM Leaves

: Biochar was prepared by the hydrothermal carbonization (HTC) of palm leaves, characterized, and utilized as an adsorbent for Malachite Green dye (MG). The Higher Heating Value (HHV) of biochar depends on the carbonization temperature and has a maximum value of 24.81 MJ/kg. Activation using H 2 O 2 oxidation of HTC biochar prepared at 208 ◦ C produced AHTC with improved capacity. The optimum pH was found to be in the range 7–8. Freundlich, Langmuir, Temkin, and Dubinin–Radushkevich adsorption isotherms were used to study MG adsorption data. The Langmuir isotherm provided the best ﬁt for experimental data. Experiments conducted using activated biochar AHTC at 25 ◦ C resulted in an adsorption capacity of 62.80 mg/g, far greater than what was observed for HTC biochar (45.59 mg/g). The maximum adsorption capacity was 88% when the concentration of MG solution was 66 ppm. The free energy change in adsorption DG ◦ indicated that the adsorption process was spontaneous. Adsorption followed pseudo-second-order kinetics. Fixed-column adsorptions models, namely, Thomas, Yan et al. and Yoon–Nelson models, were investigated for AHTC. The column adsorption capacity determined by the Thomas model was 33.57 mg/g. In addition, a computational investigation has been carried out to determine the structural and electronic features, as well as the quantum chemical parameters of HTC and MG. Moreover, the interaction between the HTC and MG is investigated, which is further elaborated by performing non-covalent interaction (NCI) through the reduced density gradient (RDG) analysis. Thus, the easily prepared hydrochar from abundant waste palm leaves can be used as a high-value biocoal and efﬁcient adsorbent of the cationic dye malachite green.


Introduction
Wastewater discharged from textiles, hair color, paper production, food technology, and leathers is usually contaminated by dyes. Thousands of tons of dyes per year are discharged into textile industry wastewater. Most synthesized dyes resist the effects of light, pH, high temperature, and microbial attack. For these reasons, biodegradation of dye is typically a slow process [1]. It is necessary to remove the dye material from the effluent before being discharged into the environment because they decrease the aesthetic value of water [2]. Recently, wastewater treatment technologies implemented novel MIL-101(Fe)/Bi 2 WO 6 microspheres [3] and Cd 0.5 Zn 0.5 S/Bi 2 MoO 6 heterostructures [4] for the photocatalytic degradation of organic compounds.
Malachite green (MG), a triphenyl methane dye, which is usually used for silk, wool, jute, and leather dying processes, has a detrimental effect on human health; it causes irritation and pain to the skin upon direct contact, irritation and even cancer of the gastrointestinal tract when inhaled or ingested [5]. The currently exhibited methods to remove this dye from effluent include coagulation, electrochemical process, membrane separation process, chemical oxidation, reverse osmosis, ozonation, chemical precipitation, and ultrafiltration, which are not popular due to their economically high cost and formation of hazardous by-products [6]. Therefore, attempts have been conducted to improve an efficient and eco-friendly technology to reduce dye content in water discharge. Adsorption is an effective and promising technique for the removal of dye from wastewater. Economic advantages and adsorption capacity are the main concerns when selecting an adsorbent; thus, current research efforts are focused on developing an efficient and low-cost adsorbent.
Recently several types of adsorbents were studied for the removal of cationic organic dyes, such as methylene blue using modified marine algae Carolina [7], crystal violet by modified Khalas dates residues [8], malachite green by hydrothermally carbonized pine needles [9] and by cobalt carbon nanostructures [10]. Crystal violet by cobalt-carbon/silica nanocomposites [11][12][13] and crystal violet and methylene blue by graphene-nickel silica [14]. In comparison, the anionic methyl orange dye was successfully removed from water by cobalt-carbon/silica nanocomposites [13]. There was an important development in the preparation and application of flexible ceramic fiber in water remediation [15]. The nanofiber/nanoparticle-based catalysts (hierarchical CuO-ZnO/SiO 2 ) showed great advantages in the treatment of Congo red and 4-nitrophenol [16]. MG pollution in aquaculture environments can be eliminated by several methods, such as adsorption, degradation using advanced oxidation processes (AOPs), or biodegradation using microbes or enzymes [17]. However, adsorption has the advantage of simplicity, low cost, and availability of adsorbents. Thus, adsorption was studied for other pollutants, such as tetracycline, using modified orange peel biochar [18] and formic acid molecules on the (104) surface of calcite [19].
Hydrothermal carbonization is a thermochemical process that transforms biomass immersed in water in an anaerobic environment and under moderate heat and pressure into carbonaceous material (HTC), which has gained less attention than the liquid product (biooil) [20,21]. The HTC process has the advance of using a non-hazardous water medium [22]. HTC products were tested recently as adsorbents; hydrothermally carbonized phycocyaninextracted algal bloom residues HTC-PE-ABR showed a high capacity for the removal of malachite green [23]. Palm leaves are abundant waste worldwide, such as in the Middle East and northern Africa regions. Millions of tons of palm leaves are naturally produced each year; the reuse of palm leaves as adsorbent for water treatment purposes can be of great economical value. The objective of this research study is to clarify the adsorption behavior of HTC and activated HTC (AHTC) prepared using palm leaves for the removal of MG in an aqueous solution. Various factors, including temperature, solution pH, and contact time, were carefully examined. The equilibrium kinetics and thermodynamics of the adsorption of MG from water were explored. The easily prepared hydrochar from abundant waste palm leaves was found to be a high-value biocoal and efficient adsorbent of the cationic dye malachite green.

Equipment and Instrument
The samples were shaken using a shaker-incubator (SHIN SAENG SKIR-601), aliquots were centrifuged with a centrifuge (Centuriol Scientific LTD), concentrations of malachite green (MG) (Figure 1a) in the supernatant were measured using UV-Visible spectroscopy (sp-3000 plus, Optima, Tokyo, Japan), the pH of the solution was measured using a pH meter (Mettler Toledo Model MP 220). Thermogravimetric-differential thermal analysis (TG-DTA) plots were measured from 20-700 • C on a SETARAM LABSYS thermal analyzer under a flow of nitrogen gas with a heating rate of 3 • C/min. High-resolution images were

Hydrothermal Carbonized Palm Leaves: HTC-PL Biochar
A stainless-steel Teflon-lined autoclave reactor of 150 mL capacity was used to prepare hydrothermal carbonization of palm leaves HTC (Figure 1b) [9]. The autoclave contained temperature and pressure sensors and a pressure relief valve. In a typical experiment, chopped pieces of palm leaves (10 g) and citric acid catalyst pellets (10 mg) were mixed in deionized water (100 mL). The autoclave was flushed with nitrogen gas. The mixture was then heated for 435 min to reach maximum temperatures Tmax (186, 201, 208, 212, or 225 °C). The temperature and pressure were recorded in intervals of 5 to 30 min for a maximum temperature of 208 °C, Figure 2a. Figure S1a shows the increase in reaction pressures (psi) versus time inside the HTC reactor at different Tmax values of 186-225 °C. In the end, the biocoal is collected by filtration, dried at 105 °C for 4 h, and weighed. HTC biochar PL-208 obtained at Tmax 208 °C was shown in Figures 2c and S1b (wet form) and Figure 2b (dry form). The processed water was weighed in order to calculate the mass balance. For the adsorption studies, the dried HTC biochar obtained at 208 °C was ground to less than 0.5 mm, chemically modified, and used as an adsorbent. The details of the preparation of adsorbent HTC-PL-208 at Tmax (208 °C) are presented in Table S1.

Hydrothermal Carbonized Palm Leaves: HTC-PL Biochar
A stainless-steel Teflon-lined autoclave reactor of 150 mL capacity was used to prepare hydrothermal carbonization of palm leaves HTC (Figure 1b) [9]. The autoclave contained temperature and pressure sensors and a pressure relief valve. In a typical experiment, chopped pieces of palm leaves (10 g) and citric acid catalyst pellets (10 mg) were mixed in deionized water (100 mL). The autoclave was flushed with nitrogen gas. The mixture was then heated for 435 min to reach maximum temperatures Tmax (186, 201, 208, 212, or 225 • C). The temperature and pressure were recorded in intervals of 5 to 30 min for a maximum temperature of 208 • C, Figure 2a. Figure S1a shows the increase in reaction pressures (psi) versus time inside the HTC reactor at different Tmax values of 186-225 • C. In the end, the biocoal is collected by filtration, dried at 105 • C for 4 h, and weighed. HTC biochar PL-208 obtained at Tmax 208 • C was shown in Figure 2c and Figure S1b (wet form) and Figure 2b (dry form). The processed water was weighed in order to calculate the mass balance. For the adsorption studies, the dried HTC biochar obtained at 208 • C was ground to less than 0.5 mm, chemically modified, and used as an adsorbent. The details of the preparation of adsorbent HTC-PL-208 at Tmax (208 • C) are presented in Table S1.

Malachite Green Solution Preparation
Analytical reagent MG, chemical formula C 23 H 26 N 2 O·HCl, λ = 618 nm, a purity of about 85%, was supplied by Sigma Aldrich. The stock solution (1 g/L) and the diluted solutions were prepared with deionized water.

Malachite Green Solution Preparation
Analytical reagent MG, chemical formula C23H26N2O·HCl, λ = 618 nm, a purity of about 85%, was supplied by Sigma Aldrich. The stock solution (1 g/L) and the diluted solutions were prepared with deionized water.

Batch Experiments
The effect of initial solution pH on adsorption was undertaken; solutions with different pH (2)(3)(4)(5)(6)(7)(8)(9) were prepared by adding 0.1 g of HTC into a 50 mL 100 ppm MG solution in a 100 mL flask. The pH of the solution was adjusted with 0.1 M HCl/NaOH. The flasks were shaken at 160 rpm and 25 °C for 24 h. The initial and equilibrium concentration of MG was determined by recording the absorbance at λ = 618 nm.
In order to study the effect of contact time, 0.1 g of HTC or AHTC was shaken with 50 mL of 100 ppm MG solution at 160 rpm at 25 °C. The absorbance was recorded at time intervals in order to determine the optimum time.

Batch Experiments
The effect of initial solution pH on adsorption was undertaken; solutions with different pH (2-9) were prepared by adding 0.1 g of HTC into a 50 mL 100 ppm MG solution in a 100 mL flask. The pH of the solution was adjusted with 0.1 M HCl/NaOH. The flasks were shaken at 160 rpm and 25 • C for 24 h. The initial and equilibrium concentration of MG was determined by recording the absorbance at λ = 618 nm.
In order to study the effect of contact time, 0.1 g of HTC or AHTC was shaken with 50 mL of 100 ppm MG solution at 160 rpm at 25 • C. The absorbance was recorded at time intervals in order to determine the optimum time.
For kinetic sorption experiments at different temperatures, 0.1 g of HTC and AHTC were added to flasks containing 50 mL of 100 ppm MG solution and then shaken at 160 rpm at pre-determined temperatures (25,30,35, and 40 • C). Aliquots of solution were taken at different times, and their absorbance was measured to determine the residual MG concentration.
While for the isothermal and thermodynamic study, a batch adsorption experiment was carried out in a shaker-incubator where 0.1 g of HTC and AHTC were added into 50 mL After shaking at 160 rpm, the remaining MG concentration of the mixture was measured.

Column Study
The experiment was conducted by packing 0.5 g of AHTC in a 1 cm wide glass column, then 100 ppm MG solution was added to the column and eluted. The height of the column bed is 0.5 cm. The flow rate was adjusted to 2 mL/min ( Figure 3). The MG concentration of the aliquot collected was determined using a spectrophotometer, and the column was operated until the column became saturated. Three cycles were carried out where the adsorbent loaded with MG was regenerated with 0.1 M HCl after each cycle.
For kinetic sorption experiments at different temperatures, 0.1 g of HTC and AHTC were added to flasks containing 50 mL of 100 ppm MG solution and then shaken at 160 rpm at pre-determined temperatures (25, 30, 35, and 40 °C). Aliquots of solution were taken at different times, and their absorbance was measured to determine the residual MG concentration.
While for the isothermal and thermodynamic study, a batch adsorption experiment was carried out in a shaker-incubator where 0.1 g of HTC and AHTC were added into 50 mL of MG solution of concentration varying from (25-200 mg/L) for 24 and 4 h, respectively. After shaking at 160 rpm, the remaining MG concentration of the mixture was measured.

Column Study
The experiment was conducted by packing 0.5 g of AHTC in a 1 cm wide glass column, then 100 ppm MG solution was added to the column and eluted. The height of the column bed is 0.5 cm. The flow rate was adjusted to 2 mL/min ( Figure 3). The MG concentration of the aliquot collected was determined using a spectrophotometer, and the column was operated until the column became saturated. Three cycles were carried out where the adsorbent loaded with MG was regenerated with 0.1 M HCl after each cycle.

Adsorption Isotherm
Equilibrium adsorption occurs in stirred batch reactors when the rate of the forward reaction (adsorption) equals the rate of the reverse reaction (desorption) [26]. The adsorption isotherm represents the distribution at the equilibrium of adsorbate molecules between the adsorbent and solution phases. It revealed the sorption mechanism, surface properties, and affinity of the sorbent [27]. Some of the equilibrium models most used in practice are Langmuir, Freundlich, Temkin, and Dubinin-Radushkevich, which were tested in this research study.

Methodology Adsorption Isotherm
Equilibrium adsorption occurs in stirred batch reactors when the rate of the forward reaction (adsorption) equals the rate of the reverse reaction (desorption) [26]. The adsorption isotherm represents the distribution at the equilibrium of adsorbate molecules between the adsorbent and solution phases. It revealed the sorption mechanism, surface properties, and affinity of the sorbent [27]. Some of the equilibrium models most used in practice are Langmuir, Freundlich, Temkin, and Dubinin-Radushkevich, which were tested in this research study. The Langmuir isotherm model assumes uniform energies of adsorption with complete monolayer coverage on the adsorbent surface [28]. The non-linear Langmuir isotherm is represented by the following equation: where Ce (mg/L) is the equilibrium concentration, qe (mg/g) is the amount adsorbed at equilibrium, q m (mg/g) is the maximum adsorption capacity, and K L is a constant related to adsorption energy. The Freundlich isotherm model [29] is the earliest known equation describing the adsorption process. It can be used for non-ideal sorption that involves heterogeneous and multilayer adsorption [30]. Freundlich model is given by the following non-linear: where K F (mg/g)(L/mg) 1/n is a distribution coefficient related to the bonding energy. nF = 1/n indicates surface heterogeneity. The Temkin isotherm model assumes that the adsorption energy decreases linearly with the surface coverage due to the interactions between the adsorbent and adsorbate [31]. The non-linear form of Temkin isotherm is given by: where b is the Temkin constant related to the heat of sorption (J/mol), K T is the Temkin isotherm constant (L/g), R is the ideal gas constant (8.314 J/K·mol), and T is the temperature in Kelvin. The Dubinin-Radushkevich (D-R) model estimates the porosity of the adsorbent and the apparent free energy of the adsorption [32]. The non-linear equations of the D-R model are shown in the following equation: where β is a constant related to the adsorption energy, q m is the theoretical saturation capacity, and ε is the Polanyi potential. The mean free energy of adsorption (E) is an indication of the nature of the adsorption process. It can be calculated from β. For values of E < 8 kJ/mol, the adsorption mechanism is controlled by physical forces; chemical forces are dominated when E is higher than 8 KJ/mol [33]. Finally, in order to evaluate the applicability of each isotherm equation, the sum of square errors (SSE) and Chi-square (χ 2 ) were calculated [34].

Preparation of HTC Biochar
The variation in the recorded temperature and pressure versus time during the hydrothermal carbonization of palm leaves to form biocoal HTC-PL208 indicated that the temperature T = 195 • C was reached quickly in 55 min. Then it increased slowly until it attained Tmax = 208 • C at 435 min ( Figure 2a). In addition, a quick increase in the pressure was observed initially until it reached 65 psi after 55 min. Then the pressure became approximately stable until it reached 90 psi at the end of the experiment after 435 min; Figure 2a for batch PL-208 at maximum temperature 208 • C and Figure S1a for all batches PL-186, PL-201, PL-208, PL-212, and PL-225 were produced at maximum temperatures Tmax ranging from 186 • C to 225 • C. The pressure increase is due to the production of gases from the dehydration and decomposition of raw biomass. Analysis, percentages, and yields for raw palm leaves and biocoal PL-208 produced by HTC prepared at Tmax = 208 • C are summarized in Table S1. Figure S2a indicated that with an increase in the maximum temperature Tmax of various hydrothermal experiments, the mass recovery decreased considerably. Therefore, in accordance with mass balance, the dry mass is reduced, whereas more dehydration (water generation) and decarboxylation (the split-off of carbon dioxide) occurred as Tmax increased [35]. This is also supported with the increase in the final pressure (affected by the generation of gas) as the final temperature of experiment Tmax increased through 186 • C, 201 • C, 208 • C, 212 • C, and 225 • C for the hydrothermal preparation of biocoal PL-186, PL-201, PL-208, PL-212 and PL-225, Figure S1a.

Properties of HTC Biochar
In addition, HTC of palm leaves produced biocoal characterized by large coal heating values (HHV), large efficiency of hydrothermal energy conversion (η), and a small rate of ash formation. The biocoal had high coal and fixed carbon yields and a low mass of volatile matter, Table 1. An important characteristic of the biocoal is the higher heating value HHV (MJ/kg). It is the total energy content released when fuel is burnt in air [36,37]. The HHV resulting from carbonization increased when the temperature of the reaction increased considerably. This increase is from 20.95 to 24.81 MJ/kg for palm leaves biochar PL-186 to PL-225 ( Table 1).
Analysis of biocoal energetic content produced showed an increase in energy conversion efficiency (η) under the effect of reaction temperature. (η) is defined as the ratio between energy content in the biocoal divided by that in the raw palm leaves; it was calculated by the relationship mentioned below, Equation (5) [38]: where η coal is the energy conversion efficiency, HHV coal is the HHV of the biocoal, and HHV bio is the HHV of the feedstock. The energy conversion efficiency η of the biocoal produced is illustrated in Table B, representing the efficiency of the hydrothermal energy conversion of dry basis biocoal to dry basis organic matter in the feedstock, which gradually increased from 79.6% to 88.7% for PL-186 to PL-225, respectively. Thus, the % energy recovery in the biocoal (i.e., energy conversion efficiency) increased with an increase in the reaction temperature at the expense of % mass recovery. The optimal reaction temperature is the maximum temperature at which the biomass has the highest energetic value without a great loss in the mass yield. This happened at a temperature of 207 • C. However, the HTC process conversion of palm leaves showed that the HHV and the % energy recovery in the bio-coal increased with an increase in reaction temperature without great loss in the mass. In addition, the HHV is most dependent on the carbon content. This confirms that HTC conversion, as a carbon concentrating process, increased the HHV of the biocoal product. The HHVs correlate well with the carbon content of the organic solids, enabling assessment of the resulting HTC-biocoal fuel characteristics. The plot of carbon content vs. calorific value (Figure 3b) Figure S2b indicated a good correlation between them. The slope was 0.537, and R 2 > 0.9. The obtained results of carbon content and calorific value of HTC Palm leaves are close to peat and brown coal [39].

Thermal and TEM Analysis of HTC and AHTC
Thermal Analysis: HTC and AHTC were heated to 800 • C, where all relevant weight loss was complete. The % mass loss and enthalpy change (J/g) at each peak temperature were shown for AHTC in Figure S3. The minor weight loss at 100 • C is due evaporation of moisture. In the first peak of HTC-PL-208 thermal analysis, 35% mass loss occurred between 150 and 350 • C at 335 • C due to organic materials decomposition and volatilization. The second peak mass loss was 40% from 350 to 550 • C was due to the coking of the carbon materials in the absence of air and the loss of significant amounts of CO 2 and CO gases. While for AHTC-PL-208, there was a mass loss of 44% in the range 150-350 • C at 327 • C and 24% at 395 • C in the range 350-550 • C, Figure S3. TGA curves indicated that the samples were not completely carbonized due to the presence of hydroxyl (-OH) and carboxylic (-COOH) groups [9].
TEM analysis: high-resolution transmission electron microscopy (HRTEM) analysis of AHTC-PL-208 showed carbonaceous sponge-like cubic mesoporous nanostructures consisting of very fine nanoparticles with sizes (<20 nm), Figure 2c. Figure 4a shows that the adsorption of MG onto HTC depends strongly on the solution pH because the adsorption capacity of MG increases with increasing pH. The maximum adsorption capacity was reached at pH = 8; lower pH results in increasing the H + concentration in the system, and hence the surface of HTC gains positive charges by abstracting H + ions. Consequently, electrostatic repulsion between the positively charged surface and the cationic dye molecules increases, which results in lower adsorption capacity; also, lower adsorption refers to the fact that H + competes with cationic dyes for the active adsorption sites on the adsorbent surface. On the contrary, the surface of the adsorbent was negatively charged at high pH, which favors the adsorption of the positively charged dye molecules due to electrostatic attraction forces [40,41]. Figure 4b presents the effect of the contact time of MG adsorption onto HTC and AHTC at 25 • C. It indicates that both HTC and AHTC reached their adsorption equilibrium at 4 h. Figure 4b shows that the curves are single, smooth, and continuous, leading to saturation, suggesting a possible monolayer layer coverage on the adsorbent surface [42]. The maximum adsorption capacity was 88% when the concentration of MG solution was 66 ppm.

Isotherm Models Computations
Experimental equilibrium data were fit to the Langmuir, Freundlich, Temkin, and Dubinin-Radushkevich models in order to find the appropriate model that best describes the adsorption process. Sorption data were analyzed according to linear Langmuir Ce/qe (g/L) vs. Ce (mg/L) Figure S4a and linear Freundlich isotherms Ln qe vs. Ln Ce (Supplementary Figure S4b). The non-linear Langmuir and Freundlich isotherms are presented in Figures S5a and S5b, respectively.
In addition, MG adsorption data onto HTC and AHTC were fit to linear Temkin isotherm qe (mg/g) vs. Ln Ce, Figure S4c, and to non-linear Temkin isotherm Figure S5c. Finally, the non-linear Dubinin-Radushkevich isotherm was plotted in Figure S5d.
From the values of SSE (smallest one) and R 2 (highest one) of four isotherm models, Table 2A, B (nonlinear) and Table S2A,B (linear). It can be noticed that the Langmuir model represents the best-fitting data for both linear and non-linear expressions. This indicated a monolayer coverage of MG on the outer surface of HTC and AHTC and that the adsorption occurred uniformly on the active adsorption sites. AHTC showed a higher adsorption capacity HTC (65.78 mg/g), which is higher than what was observed for HTC biochar at the same experimental conditions (46.08 mg/g) at 25 • C. The types of equilibrium isotherms are related to the value of R L = 1/[1 + (K L xCo)], where Co (mg/L) is the highest initial MG solution concentration studied [37]. R L values > 1 are referred for unfavorable adsorption, R L equals 1 for linear adsorption, values 0 < R L < 1 for favorable adsorption, and R L = 0 for irreversible adsorption. R L values calculated for Co = 25 ppm were found to be less than 1 and greater than 0, which suggests the favorable adsorption of MG on both HTC and AHTC. In addition, n F values from the Freundlich model were lower than 1. This also indicated strong adsorption between adsorbent and sorbate. The apparent energy E values obtained from D-R isotherm were less than 8 KJ/mol indicating the physical nature of MG

Isotherm Models Computations
Experimental equilibrium data were fit to the Langmuir, Freundlich, Temkin, and Dubinin-Radushkevich models in order to find the appropriate model that best describes the adsorption process. Sorption data were analyzed according to linear Langmuir Ce/qe (g/L) vs. Ce (mg/L) Figure S4a and linear Freundlich isotherms Ln qe vs. Ln Ce (supplementary Figure S4b). The non-linear Langmuir and Freundlich isotherms are presented in Figure S5a and S5b, respectively.
In addition, MG adsorption data onto HTC and AHTC were fit to linear Temkin isotherm qe (mg/g) vs. Ln Ce, Figure S4c, and to non-linear Temkin isotherm Figure S5c. Finally, the non-linear Dubinin-Radushkevich isotherm was plotted in Figure S5d.

Thermodynamics of Adsorption
The temperature dependency of key parameters qm and KF in the fit Langmuir and Freundlich models is shown in Figure 5. In general, the values of qm and KF increased with an increase in temperature.  The change in Gibbs free energy (ΔG°), enthalpy (ΔH°), and entropy (ΔS°) were calculated from adsorption data at four temperatures (25,30,35, and 40° C) using Van't Hoff equations [25]. The values of entropy change and enthalpy change calculated from the intercept and slope of the plot of ln K and 1/T are shown in Table 3. Where K is the equilibrium partition constant, R is the gas constant (8.314 J/K·mol), and T is the temperature in Kelvin (K). The positive value of ΔH° suggests that the adsorption was an endothermic process, and this result was confirmed by the effect of temperature on the adsorption capacity of both materials. The positive values of ΔS° show the increase in randomness at the solid-solute interface during the adsorption process, and the negative values for ΔG° at most temperatures show the feasibility and the spontaneous nature of the adsorption The change in Gibbs free energy (∆G • ), enthalpy (∆H • ), and entropy (∆S • ) were calculated from adsorption data at four temperatures (25,30,35, and 40 • C) using Van't Hoff equations [25]. The values of entropy change and enthalpy change calculated from the intercept and slope of the plot of ln K and 1/T are shown in Table 3. Where K is the equilibrium partition constant, R is the gas constant (8.314 J/K·mol), and T is the temperature in Kelvin (K). The positive value of ∆H • suggests that the adsorption was an endothermic process, and this result was confirmed by the effect of temperature on the adsorption capacity of both materials. The positive values of ∆S • show the increase in randomness at the solid-solute interface during the adsorption process, and the negative values for ∆G • at most temperatures show the feasibility and the spontaneous nature of the adsorption process. The change in the ∆G • for physical adsorption is between −20 to 0 KJ/mol, while chemical adsorption is from −400 to −80 KJ/mol [9]. The ∆G • tested at different temperatures were in the range of physisorption.

Kinetics of Adsorption
An ideal adsorbent for wastewater pollution control should have a large sorbate capacity and also reach adsorption equilibrium rapidly. Pseudo-first-order and pseudosecond-order models were tested in this research work.

Kinetics Models Computations
The linear plots of the values of log(q e − q t ) versus t ( Figure S6a) for pseudo-firstorder relationships from which q e and k 1 can be predicted from the intercept and the slope, respectively. Where q e and q t (mg/g) are the adsorption capacity at equilibrium and at time t, respectively, k 1 (L/min) is the rate constant of pseudo-first-order adsorption. This model is applicable when adsorption is preceded by diffusion through a boundary [43], and the rate of adsorption is proportional to the available sites on the adsorbent surface.
Whereas, if the pseudo-second-order model was applicable [44], then the plot of t/q t versus t ( Figure S6b) must be linear and give the values of q e and k 2 where k 2 is the rate constant of pseudo-second-order adsorption (mg/g/min). Parameters of pseudo-first and pseudo-second-order kinetics are shown in Table 4.
As can be noticed from the results, the correlation coefficients (R 2 ) for the pseudo-firstorder plot were less than that of the pseudo-second-order plot (R 2 >0.98) [45]. In addition, the fit values of q e in the pseudo-second-order model are closer to the experimental q e values. These results suggested that adsorption follows a pseudo-second-order model.

Intraparticle Diffusion Model:
The Weber-Morris intraparticle diffusion model has often been used to determine the rate-determining step [41,46], where a plot of q t versus t 1/2 should be linear if the adsorption mechanism involves intraparticle diffusion step, and it must pass through the origin if this step is the sole rate-limiting step [47]. This model also suggests that in instances when q t versus t 1/2 is multilinear, then two or more steps govern the adsorption process. Plots of q t versus t 1/2 were shown in ( Figure S6c) and ( Figure S6d). Both HTC and AHTC have the same general features of an initial linear portion with a large steeping slope k i,1 and are followed by a second linear portion with a smaller slope k i,2 [21]. The initial linear portion is attributed to bulk diffusion, and the second linear portion to intraparticle diffusion. This indicates that the transport of MG from solution through the particle solution interfaces into the pores and the adsorption on the available surface of HTC and AHTC particles are responsible for the uptake of MG. The intraparticle diffusion is the rate-controlling step only after a long contact time with rate constants due to the lower slope of the second portion of the plot. The intraparticle diffusion rate constant k i,1 ((mg/g)/min 0.5 ) at 25 • C was equal to 2.064 for HTC and 1.863 for AHTC with intercept (mg/g) 2.261 and 8.575 and R 2 0.9529 and 0.9866, respectively. The intraparticle diffusion rate constant ki,2 ((mg/g)/min 0.5 ) at 25 • C was equal to 1.060 for HTC and 0.710 for AHTC with intercept (mg/g) 9.407 and 23.039 and R 2 0.9723 and 1.0, respectively. Thermodynamics of Activation: The values of activation thermodynamic parameters E a , ∆H = , ∆S = , and ∆G = values for MG adsorption by HTC and AHTC are presented in Table 3. Using the Arrhenius equation, ln k 2 versus 1/T was plotted (Figure 6a). Using the Eyring equation, ln k 2 /T versus 1/T was plotted (Figure 6b). Where k 2 is the pseudosecond-order rate constant. The enthalpy was calculated from the slope, and the entropy from the intercept of the straight line. Physisorption has an activation energy between 5 and 40 KJ/mol, while greater values (40-800 KJ/mol) indicate chemisorption. Thus, the obtained low values of E a suggest the physical mode of adsorption of MG on both HTC and AHTC surfaces [48].

Comparison of Capacity of Prepared Biochar with Other Adsorbents
The maximum MG adsorption capacity of various adsorbents, including HTC materials, was compared with the prepared biochar in the present work HTC (45.59 mg/g) and AHTC (62.80 mg/g). It is observed that AHTC-PL has better adsorption capacity for MG compared to some other adsorbents, such as modified rice husk (15.49 mg/g) [49], rubberwood sawdust (36.45 mg/g) [50], and laboratory-activated carbons (42.18 mg/g) [51]. While "hydrothermally carbonized phycocyanin-extracted algal bloom residues" HTC-PE-ABR [23] and microalgal biochar [52] showed higher capacities of 89.05 and 166.0 mg/g, respectively. The abundance of pine needles in nature and their simple and cheap method of preparation of biochar elaborates the importance of using these materials for the removal of cationic dyes from water.
Ea, ΔH , ΔS , and ΔG values for MG adsorption by HTC and AHTC are presented in Table  3. Using the Arrhenius equation, ln k2 versus 1/T was plotted (Figure 6a). Using the Eyring equation, ln k2/T versus 1/T was plotted (Figure 6b). Where k2 is the pseudo-second-order rate constant. The enthalpy was calculated from the slope, and the entropy from the intercept of the straight line. Physisorption has an activation energy between 5 and 40 KJ/mol, while greater values (40-800 KJ/mol) indicate chemisorption. Thus, the obtained low values of Ea suggest the physical mode of adsorption of MG on both HTC and AHTC surfaces [48].

Adsorption in a Fixed Bed Column
The study of sorption kinetics in wastewater treatment is important since it provides valuable insights into the reaction pathways and mechanism of adsorption [29]. In order to examine the mechanism of the adsorption process, a suitable kinetic model is needed to analyze rate data. Three models (Yoon and Nelson, Thomas, and Yan et al.) [8][9][10][11][12][13][14]25,37] were used to analyze the column performance for the removal of MG from an aqueous solution. The Thomas kinetic model assumes that the process follows Langmuir kinetics of adsorption-desorption with no axial dispersion [53]. It describes that the rate driving force obeys second-order reversible reaction kinetics. The linear form of the Thomas model is given in Equation (6).
where k T (mL/mg·min) is the Thomas rate constant, q T (mg/g) is the equilibrium adsorbate uptake, Q is the flow rate (mL/min), C o is the initial dye concentration, C e is the dye concentration in the effluent and m (g) is the mass of the adsorbent in the column. Experimental data were fit to the Thomas model. The rate constant k t and the maximum capacity of sorption q T values were calculated from the slope and intercepts of linear plots of ln[(C o /C e ) − 1] against t (min). The Yoon and Nelson Kinetic Model investigates the breakthrough behavior of adsorbate onto the adsorbent surface [54]. The linear Yoon and Nelson model is expressed in Equation (7): where k YN (min −1 ) is the rate constant, and τ is the time required for 50% adsorbate breakthrough. The linear plot of ln[Ce/(C o − C e )] against time (t), values of k YN , and τ were obtained from the intercept and slope of the plot, respectively. The empirical equation proposed by Yan et al. [55] was found to provide a better description of the breakthrough curves in a fixed column. The linearized Yan et al. equation is expressed in Equation (8): where k y is the kinetic rate constant for Yan Model (mL·min −1 ·mg −1 ), and q y is the maximum adsorption capacity (mg·g −1 ) of the adsorbent.
The area under the breakthrough curve gives the total adsorbed mass of MG dye (q total ) in mg in the column. It can be calculated from the following integration [56]: where t is the time (min), and Q is the volumetric flow rate (mL/min). The maximum capacity of the column can be calculated: q max (mg/g) = q total /m, where m is the sorbent mass (g). The column uptake capacity q max for the first cycle was calculated to be 15.468 mg/g using the area under the breakthrough curve method Equation (9). Figure 7a shows the breakthrough curve obtained for MG adsorption on AHTC for three column cycles. Column studies showed lower removal capacity than that obtained by batch adsorption due to shorter contact time between the adsorbate and adsorbent. Figure 7b shows the uptake efficiency (% removed) of the three cycles where the decrease in efficiency was not valuable. AHTC can be used repeatedly without significant loss of sorption capacity upon regeneration with 0.1 M HCl (100 mL), showing its feasibility for commercial application, Figure 7c.
to shorter contact time between the adsorbate and adsorbent. Figure 7b shows the uptake efficiency (% removed) of the three cycles where the decrease in efficiency was not valuable. AHTC can be used repeatedly without significant loss of sorption capacity upon regeneration with 0.1 M HCl (100 mL), showing its feasibility for commercial application, Figure 7c.  Figure S7a, and nonlinear Thomas model Figure S7b.
The Thomas and Yoon-Nelson models showed higher fitting than Yan's model with R 2 > 0.98. Thus, the highest sorbent capacity given by the Thomas model was qT 33.60 and 33.57 mg/g for linear and nonlinear models, and the rate constants kT were 0.606 and 0.330 (mL·mg −1 ·min −1 ). The highest breakthrough time for 50% removal estimated by the Yoon-Nelson model (linear and nonlinear) was averaged at 48.2 min, while the rate constant  Figure S7a, and nonlinear Thomas model Figure S7b.
The Thomas and Yoon-Nelson models showed higher fitting than Yan's model with R 2 > 0.98. Thus, the highest sorbent capacity given by the Thomas model was q T 33.60 and 33.57 mg/g for linear and nonlinear models, and the rate constants k T were 0.606 and 0.330 (mL·mg −1 ·min −1 ). The highest breakthrough time for 50% removal estimated by the Yoon-Nelson model (linear and nonlinear) was averaged at 48.2 min, while the rate constant K YN was 0.059 (min −1 ). The capacity q Y and rate constant k Y for Yan et al. (linear model) were 6.083 (mg·g −1 ) and 45.844 (mL·mg −1 ·min −1 ).

Computational Methods and Investigations
The interaction between hydrochar adsorbent and malachite green adsorbant has been explored by DFT computation in order to support the adsorption isotherms and kinetics results. Density functional theory (DFT) [57] calculations were performed using Gaussian 16 (revision C.01) [58], and Gaussview [59] was used to generate input geometries and visualize output structures. Regarding geometry optimizations and frequency calculations for HTC and MG, ωB97XD [60] was functionally implemented in the Gaussian program and was used with the 6-311(d, p) basis set. All stationary points were characterized as minima, and thermal corrections were computed from unscaled frequencies, assuming a standard state of 298.15 K and 1 atm. To account for the presence of non-covalent interactions, reduced density gradient (RDG) analysis [61] was performed using the Multiwfn program [62] and visualized by visual molecular dynamics (VMD) [63].
The computational investigation is instrumental in determining the theoretical parameters which are directly associated with envisaging the reactivity behavior of organic molecules, and these parameters have been extensively studied to illustrate the interactions between the surface of adsorbents and dyes [64][65][66][67] These reactivity descriptors include E HOMO , E LUMO , ionization potential (I), and electron affinity (A). Both I and A can directly be calculated using the E HOMO and E LUMO as described in Equations (26) and (27) [68].
The values of ionization potential (I) and electron affinity (A) are used to calculate other fundamental reactivity parameters, including chemical hardness (η), electronic chemical potential (µ), and electrophilicity index (ω) as reported in the literature [66,69,70].
These parameters provide useful insight to analyze the dye/surface interaction through understanding the reactivity behavior of soft and hard acid-base theory. The concept of chemical hardness (η) is a direct indicator of reactivity, and in general, the molecules with low chemical hardness are more reactive [71]. The electronic chemical potential (µ) highlights the potential of a compound to exchange electronic density with other chemical species. The higher the value of chemical potential, the higher the ability of a molecule to act as a strong electron acceptor [63]. In addition, the electrophilicity index (ω) is a measure of energy lowering due to maximal electronic flow between donor and acceptor. The tendency of a molecule to accept the loading of electrons is explained by this reactivity descriptor [63].
The computed values for these chemical reactivity parameters for the adsorbent (HTC) and the dye (MG) are presented in Table 5. These values provide theoretical data which will be exploited further when compared with the adsorbent behavior of HTC for other dyes. The optimized geometries of HTC and MG are presented in Figure 8a. Frontier molecular orbital analyses for HTC and MG are provided in Figure 8b, which reveal that the HOMO of HTC is uniformly and predominantly located on the adjacent furan rings. The energy gap for HTC is 6.34 eV. In the case of MG, the energy gap between HOMO and LUMO is 5.22 eV, while the position of HOMO is on the chloride ion and adjacent aromatic ring. In addition, and as expected, ESP maps for HTC and MG illustrate the presence of active sites, which play a pivotal role in the strong interaction between both, Figure 8c. For HTC, the most electron-rich sites are located on oxygen atoms present in the molecule, while in the case of MG, it is uniformly spread over the electrons containing aromatic rings.
Next, we investigated the interaction between HTC and MG Figure 9. The optimized geometry for the adsorption of MG over HTC was calculated and shown by a favorable interaction. The adsorption free energy was calculated to be exergonic at 6.7 kcal/mol at 298.15 K. The electronic adsorption energy was highly negative at 27.7 kcal/mol Figure 9a. These results indicate the possible favorable interaction of MG over HTC. The nature of the interaction was further confirmed by computing the non-covalent interaction (NCI) through the reduced density gradient (RDG) analysis Figure 9b. The results of NCI show a great CH-π interaction between the aromatic rings of MG and the methylene groups on the HTC. The optimized geometries of HTC and MG are presented in Figure 8a. Frontier molecular orbital analyses for HTC and MG are provided in Figure 8b, which reveal that the HOMO of HTC is uniformly and predominantly located on the adjacent furan rings. The energy gap for HTC is 6.34 eV. In the case of MG, the energy gap between HOMO and LUMO is 5.22 eV, while the position of HOMO is on the chloride ion and adjacent aromatic ring. In addition, and as expected, ESP maps for HTC and MG illustrate the presence of active sites, which play a pivotal role in the strong interaction between both, Figure 8c. For HTC, the most electron-rich sites are located on oxygen atoms present in the molecule, while in the case of MG, it is uniformly spread over the electrons containing aromatic rings.  Tables S3 and S4. Next, we investigated the interaction between HTC and MG Figure 9. The optimized geometry for the adsorption of MG over HTC was calculated and shown by a favorable interaction. The adsorption free energy was calculated to be exergonic at 6.7 kcal/mol at 298.15 K. The electronic adsorption energy was highly negative at 27.7 kcal/mol Figure 9a. These results indicate the possible favorable interaction of MG over HTC. The nature of the interaction was further confirmed by computing the non-covalent interaction (NCI) through the reduced density gradient (RDG) analysis Figure 9b. The results of NCI show a great CH-π interaction between the aromatic rings of MG and the methylene groups on the HTC.  Tables S3 and S4.

Conclusions
This project used a readily available, abundant waste biomass (palm leaves), hydrothermally treating it to form HTC adsorbent and chemically activating it into useful adsorbent AHTC in a cheap and simple way. HTC preparation setup and energetic properties of hydrothermal carbonized palm leaves were investigated. The HHV of hydrochar resulting from carbonization was 24.81 MJ/kg. It increased when the temperature of the reaction increased. This study shows that the hydrochars prepared at 208 °C, HTC and

Conclusions
This project used a readily available, abundant waste biomass (palm leaves), hydrothermally treating it to form HTC adsorbent and chemically activating it into useful adsorbent AHTC in a cheap and simple way. HTC preparation setup and energetic properties of hydrothermal carbonized palm leaves were investigated. The HHV of hydrochar resulting from carbonization was 24.81 MJ/kg. It increased when the temperature of the reaction increased. This study shows that the hydrochars prepared at 208 • C, HTC and AHTC, are efficient adsorbents of MG from an aqueous solution. H 2 O 2 improved the MG removal ability of HTC. The obtained capacity of AHTC was 65.78 mg/g. The sorption kinetics obeyed the pseudo-second-order model. Langmuir isotherm had the best fit to equilibrium data for MG adsorption, indicating a monolayer coverage mode. R L values show that the sorption process is favorable. The free energy change of adsorption ∆G • indicated that the adsorption process is spontaneous. We also proved the successful application of a column packed with AHTC palm leaves for continuous removal of pollutants with no noticeable deterioration of adsorbent, which was also regenerated and reused in three cycles. The Thomas column adsorption capacity was found to be equal to 16.48 mg/g. Thus, the prepared adsorbent can find application in industry.
The structural and electronic aspects of HTC and MG were further elaborated by performing computational studies related to frontier molecular orbital and electrostatic potential map analyses. The interaction between HTC and MG was also computed, and the value of electronic adsorption energy confirms the possible favorable interaction of MG over HTC. Furthermore, the nature of the interaction was iso determined by computing non-covalent interaction (NCI) via the reduced density gradient (RDG) analysis.