International Journal of Chemical Engineering

International Journal of Chemical Engineering / 2021 / Article
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Thermochemical, Biochemical, and Chemical Conversion of Biomass into Value Added Materials

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Research Article | Open Access

Volume 2021 |Article ID 5555406 |

Faiçal El Ouadrhiri, Majda Elyemni, Amal Lahkimi, Abdelhadi Lhassani, Mehdi Chaouch, Mustapha Taleb, "Mesoporous Carbon from Optimized Date Stone Hydrochar by Catalytic Hydrothermal Carbonization Using Response Surface Methodology: Application to Dyes Adsorption", International Journal of Chemical Engineering, vol. 2021, Article ID 5555406, 16 pages, 2021.

Mesoporous Carbon from Optimized Date Stone Hydrochar by Catalytic Hydrothermal Carbonization Using Response Surface Methodology: Application to Dyes Adsorption

Academic Editor: Mohamed Zbair
Received29 Jan 2021
Revised27 Mar 2021
Accepted02 Apr 2021
Published22 Apr 2021


Providing efficient and environmental friendly ways to recover lignocellulosic waste remains a challenge around the world. In this study, citric acid-catalyzed hydrothermal carbonization (CHTC) was coupled with pyrolysis to convert date seed (Ds) into adsorbent material. In this regard, a central composite design (CCD) using response surface methodology (RSM) was developed to examine the influence of temperature, reaction time, and catalyst dose on the mass yield (Ym(%)) and carbon retention rate (CRR(%)) in the produced hydrochars. The optimized hydrochar (OHC-Ds) was obtained under optimal conditions (200°C, 120 min, 20 mg) and characterized by a Ym(%) and CRR(%) of 59.71% and 75.84%, respectively. Chemical activation by KOH of OHC-Ds followed by pyrolysis at 600°C resulted in an active material (AOHC-Ds) rich in carbon and characterized by a high specific surface area of 1251.5 m2/g, with the dominance of mesopores, as well as an amorphous structure comparable to graphite shown by X-ray diffraction (XRD) analysis. Adsorption experiments of two dyes on AOHC-Ds showed a high maximum adsorption capacity (Qm) of 657.89 mg g−1 for methylene blue (MB) and 384.61 mg g−1 for methyl orange (MO) compared to other conventional adsorbents. This result is due to the low acidity (pHpzc) of the surface of AOHC-Ds, which equals 6.75, and its surface, which is also rich in oxygenated functional groups such as (-OH), (C=O), and (C-O) shown by FTIR analysis. These results suggest that the coupling of CHTC and KOH activation followed by pyrolysis is an encouraging way to prepare an efficient and inexpensive adsorbent to remove dyes in wastewater.

1. Introduction

An unprecedented challenge in the field of energy and the environment marks the beginning of the twenty-first century. With 81% of the worlds energy supply dependent on fossil fuels [1], problems of depletion or explosion costs are looming on the horizon. Besides, the use of fossil fuels contributes to the development of greenhouse gases, which, according to the majority of the scientific community, are responsible for many climate changes on a planetary scale [2]. According to the World Health Organization (WHO), it is estimated that soon 2/3 of the population could live in a region with limited access to water [3]. In order to remedy this problem, one of the options being considered is the reuse of wastewater even after passing through a treatment plant, especially for agriculture, which is the sector that consumes the most water [3]. Therefore, the problem is twofold: to meet the growing need for water and try to preserve our environment. Indeed, several molecules and compounds are present in wastewater, namely, hydrocarbons, dyes, heavy metals, xenobiotic molecules (endocrine disruptors), and pesticides [4]. Some of them are carcinogenic and contribute to the degradation of the environment and human health [5]. In this sense, many technologies have been innovated to decontaminate the wastewater and reduce pollution. Among them, adsorption has aroused great interest, since it has a high contaminant removal capacity and broad adsorbent-adsorbate selectivity [6]. Among the various adsorbents used, activated carbon (AC) is the most used for these many properties [7]. The increasing demand for activated carbon leads to intensive research into renewable precursors’ production, mainly biomass, for their production [8]. Biomass has many advantages, not only in terms of abundance and distribution but also in terms of its conversion/recovery using a wide range of technologies: thermal (direct combustion) to produce heat and electricity, as well as for the production of electricity [9], thermochemical (gasification, pyrolysis, and hydrothermal carbonization) [10], and biological (anaerobic digestion and fermentation), its simplicity of execution, the removal of energy-intensive drying processes, and greenhouse gas emissions reduction. In recent years, significant attention has been paid to hydrothermal carbonization (HTC) as a promising method of conversion that can recycle waste, lead to low-cost development of new porous materials, and respond to specific environmental challenges [11].

The world production of dates is still increasing. In Morocco, the annual production is around 160,000 tons of dates, making it in the 3rd place among the Maghreb countries and the 7th in the world [12]. Date seeds have several uses in various fields. For example, the use of the oil extracted from date seed in cosmetics and also the grounded seeds are used as an additive to coffee. In fact, a study [13] showed that the aqueous extract of date seeds has an antigenotoxic effect. Despite its uses, date seeds are still considered waste and thrown away either by consumers or industrialists without valorization. According to [14], date seeds contain about 57% cellulose, 23% hemicellulose, and 15% lignin [14]. This is why it is crucial to find a new and appropriate way to enhance the value of date seeds.

In the recent literature, several studies have been conducted to manufacture adsorbents from date seeds using classical production methods such as pyrolysis or gasification followed by chemical or physical activation or coupling between them [15]. To the best of our knowledge, no studies have shown the use of the catalyzed hydrothermal carbonization process (CHTC) using citric acid in the preparation of adsorbent materials from date seeds. However, activated carbon from date seeds via HTC coupled with chemical activation by NaOH has been reported by [16]. According to [17], the two parameters that have an important influence are the temperature and the reaction time as well as the pH of the reaction which is little studied in the literature. In this study, the preparation of a carbon-rich material from date seeds using citric acid-catalyzed hydrothermal carbonization and their dye adsorption application have been the innovative outlooks.

More specifically, the objectives of this study are(i)The optimization of the CHTC operating parameters (temperature, reaction time, and catalyst dose) on mass yield (Ym(%)) and carbon retention rate (CRR(%)) in hydrochar produced from date seeds using RSM coupled with CCD design(ii)The preparation of the active material from the optimized hydrochar was prepared by the KOH impregnation method reported by [18] with modification(iii)The evaluation of the capacity of the activated material (AOHC-Ds) on the adsorption of a cationic dye (methylene blue: C16H18ClN3S) and an anionic dye (methyl orange: C14H14N3NaO3S), which represent the most dyes used in the industry [19]

This study, through the various techniques employed, such as elemental analysis (CHNO), surface chemistry (FTIR), porosity analysis, X-ray diffraction (XRD), and pH at zero points of charge (pHpzc), has clearly shown that the integration of CHTC is an encouraging way to convert date seeds into a carbonaceous material that is highly efficient in the removal of dyes in water.

2. Materials and Methods

2.1. Collection and Preparation of Raw Material

The date seeds (Ds) chosen in this study as a precursor were obtained from the local market in Fez, Morocco. First, seeds were washed with distilled water (DW) and put in an oven at 65°C for 12 hours, ground in a GM200 grinder (Retsch, GmbH, Germany), sieved to obtain a particle size fraction of 500 μm < d < 250 μm (60–35 mesh) for better decomposition in the CHTC process, and finally stored in a desiccator for later use. NaOH and HCl used in this work are analytical grade. Citric acid was ACS reagent grade with a purity of ≥99.5% (Sigma-Aldrich, Inc.).

2.2. Hydrothermal Carbonization (HTC)
2.2.1. Synthesis of Hydrochars

The hydrothermal carbonization of date seeds was carried out in a polypropylene-lined (PPL) autoclave with a volume of 100 mL. In each experiment, 8 g of the Ds powder was mixed with 80 mL of DW to have a biomass/water ratio of 1 : 10 with stirring for 10 min. A precise mass between 10 mg and 20 mg of citric acid (C6H8O7) as an acid catalyst was added to the mixture during stirring and then loaded into the reactor and well sealed. The autoclave was transferred to an oven and heated to the target temperature for a specific time (40–140 min). All experiments were carried out at a constant heating rate of 5°C/min. After the reaction, the autoclave was cooled naturally, and the hydrochar is recovered by centrifugation, washed with DW, dried at 105°C overnight, and stored. The hydrochar is named HC-NDx (x, number of experiments).

2.2.2. Hydrochar Activation

The optimized hydrochar selected in the optimization part was chemically activated by the KOH impregnation method reported by [18, 20]. 5 g of OHC-Ds were impregnated with 100 mL of KOH (2 M) solution for 4 hours at room temperature and continuous stirring and then dried in the oven at 60°C overnight. Finally, the powder obtained was sintered in a muffle furnace at 600°C, for one hour. The final activated material named AOHC-Ds was washed with DW and dried in the oven overnight and then stored.

2.3. Design of the CCD/RSM

Design of experiments (Doe) and response surface methodology (RSM) are useful tools for studying, developing, and optimizing a wide range of engineering systems [21]. The Doe approach using RSM is a robust tool for understanding and optimizing experimental parameters, allowing a rational interpretation of their influence on the selected responses with a considerable reduction in the number of experiments and an improved understanding of the process mechanism [22]. In this work, the effect of temperature (X1), reaction time (X2), and catalyst dose (X3) on two responses, mass yield (Ym(%)) and carbon retention rate (CRR(%)), has been described by a quadratic polynomial model using the following equation, including linear effects, interaction effects, and quadratic effects, i.e., for k independent factors:where is the measured response to the experiment i. β is the constant regression coefficient. and are the independent coded prediction variables called factors. design the difference between the observed and estimated values of the measured response called total error.

Based on the central composite design (CCD) using Expert–Design software, which is one of the most used matrices due to its good performance and minimum number of experiments [23], 20 experiments were suggested for k = 3 factors according to the following equation:

Include (2k = 8) experiments corresponding to the factorial design (2k = 6) experiments located on the axes and (N0 = 6) experiments at the center of the domain. The latter was chosen equal to six to determine the experimental error and ensure the accuracy and reliability of our model at any point of the experimental domain. In order to account for any randomized hidden effects, the experiments were conducted in the random order (Table 1S). Figure 1S shows the geometric location of the experimental points of the CCD design. The levels used −α, −1.0, +1, and +α for the three variables in the CCD design of which α = (2k)1/4 = 1.682 to ensure the isovariance property by rotation of the design, as presented in Table 1.

Variable nameCode−1.68 (−α)+1.68 (+α)Coded lowCoded highMeanStd. deviation

A = temperature (°C)X1166.36233−1 ↔ 180.00+1 ↔ 220.00200.0016.96
B = reaction time (min)X240140−1 ↔ 60.00+1 ↔ 120.0090.0025.43
C = catalyst dose (mg)X313.3021.70−1 ↔ 15.00+1 ↔ 20.0017.502.12

Once the modeling is complete, the final step of the study is optimization, which consists of finding the response functions optimal levels. Several optimization methods can be used to simultaneously optimize the two studied responses resulting from the use of the response surface method. In this study, the numerical method was applied using the desirability function (D). This methods choice is taken because it gives us the possibility to modify the weight and importance either for the variables or the responses. Besides, all these criteria were combined in a single desirability function (D) [24]. The software allows us to estimate the predicted values by the value of D varying from 0 to 1 with perfect values when d = 1 [25].

2.4. Characterization

The elemental analysis of carbon (C), hydrogen (H), nitrogen (N), and sulfur (S) was carried out in an apparatus (2400 CHN Elemental Analyzer, Perkin-Elmer, France), and the percentage of oxygen was calculated by subtraction. The prediction of the higher heat value (HHV) was made using the unified model (equation (3)) developed by [26], which is based on elemental analysis and which involved more variables in the prediction of the calorific values of our samples [27, 28]. The Ym(%) and CRR(%) are the two responses studied in order to optimize them. The Ym(%) was calculated by equation (4) according to [29, 30]. CRR(%) is defined as the fraction of carbon in the hydrochar (% Chydrochar) to that of the initial biomass (% Craw biomass). This response was calculated using equation (5) as ratios by [31, 32]

The textural characteristics of OHC-Ds and AOHC-Ds were determined by the isotherms of nitrogen physisorption at 77.35 K using an ASAP 2020 manometric analyzer (Micromeritics, USA). The specific surface area was calculated by the Brunauer–Emmett–Teller (BET) method in the range of 0.05–0.35. The total pore volume Vp was obtained from the amount of absorbed nitrogen at P/P0 ≈ 0.99. The micropore volume Vmicro was calculated using the t-plot method with the thickness t which equals specific for carbon-based materials [33]. The mesoporous volume Vmeso was deduced by subtraction Vméso = Vmicro − Vp. The pore size distribution was determined by the Barrett–Joyner–Halenda (BJH) method [34]. Besides, the pores average diameter (Dp) was calculated by assimilating them to a cylindrical shape [35]. The functional groups of the raw biomass surface, carbon material, and changes due to the HTC process were demonstrated by a Fourier transform infrared spectroscopy (FTIR) (Perkin Elmer, USA). Samples for measurements were prepared using the KBr disc method in the range 500–4000 cm−1. The identification of the crystalline phases (position and intensity of the diffracted lines) was carried out by X-ray diffraction (XRD) using a Bruker D Discover diffractometer (Germany), equipped with Cu-Kα radiation (1.54 Å), covering an angular range from 5° to 50° with a step of 0.05°. The pHpzc (zero charge point) is defined as the pH value when the materials surface charge is zero. The pHpzc of the AOHC-Ds was determined by the pH drift method described in supporting information (SI), the most accurate method according to [36, 37].

2.5. MB and MO Adsorption Test onto AOHC-Ds

AOHC-Ds were used as an adsorbent for the removal of methyl orange and methylene blue from water. The effect of pH on MB and MO removal rate through AOHC-Ds was achieved in the range 2–12. The solution pH was adjusted either by the addition of HCl (0.1 M) or NaOH (0.1 M). The influence of the AOHC-Ds dose in the range 2.5–25 mg, the initial concentration of MB and MO in the range 25–900 mg L−1, and the contact time in the range 0–60 min were performed in batches in 100 mL volumetric flasks under constant magnetic agitation. After each test, the supernatants’ concentration was determined using a UV-visible spectrophotometer at wavelength 465 nm for MO and 664 nm for MB. By preparing MB and MO concentrations from 0 mg L−1 to 10 mg L−1, from a stock solution of concentration 1 g·L−1 (Cstock = 1 g·L−1), a calibration curve was made with a coefficient R2(MB) = 0.999 and R2(MO) = 0.998. The equations applied for the calculation of the adsorption removal rate R%, the adsorption capacity Qe, as well as the two adsorption models used in this work are presented in Table 6S.

3. Results and Discussion

3.1. Modeling and Analysis of the Statistical Properties of the CHTC Process

In this study, RSM coupled with the CCD plan was used to describe the variation in interest responses as a function of factor fluctuations and determine the factors involved in achieving the original objectives. The quality assessment of each model was tested using the analysis of variance (ANOVA) by the Fishers test (F value), the probability p ( value), and the significance of the lack of fit to determine whether the model correctly summarizes the results of the design of experiment tests [21]. The regression models fit the evaluation of its predictive qualities, and its operation was verified using the correlation coefficient of the multilinear regression (R-squared), helpful in describing the variation in the experimental data that the model explains. This coefficient can be misleading for evaluating the fit of the model predicted. For this reason, the coefficient adjusted and the coefficient predicted were introduced into the evaluation to determine the model’s ability to predict new observations. In addition, normal residual and predicted versus normal value plots were used to assess the residuals distribution and normality.

3.1.1. Model Ym(%)

The experimental values of the CCD matrix of mass yield experiments presented in Table 1S allowed the mathematical model to be adjusted by the least-squares procedure. The analysis of variance ANOVA in Table 2S shows that the mass yield regression is very significant with an F value of 349.33 and value < 0.0001, on the one hand, and on the other hand, the lack of fit (F value of 2.09) is not statistically significant compared to the pure error. Moreover, the R2 coefficient of the predicted model is 0.9968, which affirms the correlation and good fit between the experimental and calculated data. This is also confirmed by the difference between the (0.9940) and the (0.9818), which is reasonable given that it is less than 0.2. The coefficient of variance (CV%) for Ym(%) is 0.65%, which indicates that the model is capable of better prediction. The ANOVA analysis for the coded terms shows that only the temperature (), the term of the interaction , and the quadratic term of the catalyst dose () have a significant influence on hydrochar mass yield given that their value is less than 0.05. In addition, values of other terms greater than 0.1 reveal that these terms are statistically insignificant. Consequently, only the effects of the significant terms were considered in the following equation in terms of factors coded to predict mass yield values, namely,

Indeed, the terms (), , and () have quite a negative effect on the mass yield with a negative coefficient of −5.79, −0.24, and −0.29, respectively. In the same context, the normal plot of the residuals shown in Figure 1(a) indicates that the residue points distribution correctly follows the straight line, which justifies that the distribution is homogeneous. Besides, the importance of the experimental values was verified by plotting the predicted vs. actual plot. Figure 1(b) shows that the set of values was distributed close together around the diagonal line, which affirms the predicted model’s accuracy and validity. The 3D response surface graphs obtained from equation (6) for the mass yield are shown in Figure 2S, showing that there is a wide range of variables for which the mass yield is almost flat in the range 160°C < T < 240°C, 32 min < t < 120 min for a fixed catalyst dose equal to 17.5 mg. For example, the mass yield in hydrochar increased from 67.9% to 49.2% by varying the temperature from 165°C to 235°C. In general, for XA − XB values, an increase in these two variables leads to a slight decrease in the hydrochar Ym(%). Our results are in agreement with those reported on hydrothermal carbonization of biomass [3840].

These results can be explained by the dehydration, condensation, polymerization, and aromatization reactions during hydrothermal processing of the cellulose and hemicellulose contained in the biomass matrix [41, 42]. In addition, the hydrochar mass yield by the HTC process in the case of the date seed is much higher with biomass conversion techniques such as pyrolysis [43, 44] and gasification. On the other hand, the 2D and 3D graphs in Figures 1(c) and 1(d) show that the temperature increase and the catalyst dose (XC) in the range 160°C < XT < 240°C, 14 mg < XC < 21 mg for a fixed time of 120 min have a negative and little noticeable effect on the mass yield of hydrochar. It is concluded that while temperature and time play the leading role in the HTC process, the mass yield decreased as the dose of citric acid increased. Our results are very similar to [45], to maize silage [39], and to salacca peel and not in the case of resin pulp [46].

3.1.2. Model CRR(%)

The carbon recovery rate is defined as the amount of carbon in the hydrochar relative to the amount of carbon in the biomass [32]. The RSM was used to determine the relationship between CRR(%) and the three variables studied. The ANOVA analysis is presented in Table 3S. As we can see, on the one hand, the coefficient of 0.8561 is in reasonable agreement with (0.9541). On the other hand, the R2 coefficient is 0.9759, indicating the model’s excellent fit to the experimental data. Moreover, compared to the pure error, the F value of the lack of fit is 2.48, which means that the lack of fit is not important, with a CV% of 0.98, which shows that the model explains well the totality of the experimental data. Indeed, from the value values of the coded terms, we can conclude that temperature (), time (), the dose of citric acid (), and the quadratic terms () and () are the only terms statistically significant for CRR(%). Then, the final equation (equation (7)) of the quadratic model for the carbon recovery rate in terms of the coded variables is

Regarding the validity and correctness of the model, it can be seen that not only the distribution of the points around the straight line in the normal plot (Figure 2(a)) is homogeneous but also the actual values were distributed evenly from the diagonal in the predicted vs. actual plot (Figure 2(b)). The relationship between the variables (temperature, time, and nitric acid dose) was established using equation (7) via the 3D and 2D response surface plots. The plots parabolic shape in Figures 2(c) and 2(d) shows the influence of temperature and time on the carbon recovery rate. As can be seen, the optimum operating point of the process, located within the experimental range of the studied variables, corresponds to the cones stationary point. For example, passing from a temperature of 150–230°C for a fixed reaction time (120 min), we observe the passage of CRR(%) through an optimum region hatched in red. These findings are consistent with those of [38, 47, 48]. However, Figure 3S shows that at lower temperatures (180–200°C), we find that CRR(%) increases with increasing dose of citric acid, which is consistent with the conclusions of the study [49], in the case of pure cellulose. The only possible reason for these conclusions is that the CHTC process increases CRR(%) in hydrochars and the citric acid that penetrates in the biomass matrix and thus causes the hydrolysis of cellulose, hemicellulose, and lignin. Indeed, the carbon contained in the citric acid can be adsorbed in the surface of the hydrochars, according to the study of [50], which makes the hydrochar much rich in carbon during catalyzed hydrothermal carbonization.

3.2. Numerical Optimization of the HTC Process Using the Desirability Function

Among the objectives of this study is developing a hydrochar from date seeds with controlled properties, particularly a carbon recovery rate and mass yield, which must be as high as possible. Using RSM/CCD, we have established the relationship between the process variables and the interest responses via the validated mathematical model and response surface graphs. However, the present study used the desirability function to determine the optimal level of carbon recovery rate in hydrochar with the constraints cited in Table 4S. Among the 27 solutions calculated by the software, function D highest value is chosen as the optimal solution. Figure 4S shows the variation of the highest desirability function (88.70%) corresponding to the values (XA = 200°C, XB = 120 min, and XC = 20 mg). Under these conditions, the experiments presented in Table 2 show a carbon recovery rate of 74.84% and a mass efficiency of 60.1% with a percentage error of 2% and 1.7%, respectively. It means that both models predicted using RSM/CCD reasonably follow the experimental data. Finally, the hydrochar-optimized OHC-Ds under the conditions XA = 200°C, XB = 120 min, and XC = 20 mg suffered chemical activation as detailed in the hardware and method section.

XA = 200°C, XB = 120 min, and XC = 20 mg (desirability function = 88.70%)

Ym%58.5359.711.18 (2%)
CRR%77.1975.841.35 (1.7%)

Percentage error between experimental and model-predicted values.
3.3. Characterization of Hydrochars
3.3.1. CHNO Analysis

The elemental analysis presented in Table 5S indicates that the percentage of carbon increased significantly during the HTC process with a maximum of 69.03% for HC-ND17, which has a positive effect on the textural and adsorption properties of AOHC-Ds after chemical activation, according to [51]. On the other hand, the percentage of oxygen decreased by about 60% due to dehydration and decarboxylation reactions. These findings are consistent with the conclusions of [52], which used strong acids (HCl, H2SO4, and HNO3) to convert bamboo Moso into hydrochar using HTC. The atomic O/C and H/C ratios of the hydrochar and raw biomass were calculated using the elemental analysis and presented using the van Krevelen diagram [53] for purposes of comparison with other materials and to get an idea of the degree of carbonization.

As shown in Figure 3, the position of the hydrochars is between lignite, bituminous coal, and charcoal at the bottom and cellulose and wood at the top. It can also be seen that the atomic ratios follow a diagonal line, which indicates that the predominant reaction in the conversion of date seed to hydrochar using citric acid-catalyzed HTC is dehydration and decarboxylation. It is also noted that by increasing the temperature from 200°C to 233°C, the conversion is characterized by a demethanization reaction, thus revealing the effect of citric acid in the formation of hydrochars, which is in agreement with the study of [52]. Another interesting remark is that the energy power represented by the higher heating value (HHV) of all samples was increased by about 70%, which is interesting from an energy point of view. The results of this study for HHV are almost the same as several studies [54], in the case of grape marc [55], in the case of woody biomass, and for macrophyte Hornwort [56], who showed that the catalyzed HTC process had a direct positive effect on the energetic properties of hydrochars, whether it be the nature of the raw material or the operating conditions.

3.3.2. Porosity and Pore Size Distribution

The adsorption-desorption isotherm of liquid nitrogen at 77 K of AOHC-Ds and OHC-Ds is shown in Figure 4. The isotherm of AOHC-Ds is type IV typical of mesoporous materials [57]. According to the IUPAC classification, a hysteresis loop type H4 accompanies the presence of capillary condensation in the partial pressure region (0.45–0.99) on its desorption branch [58]. This result indicates that AOHC-Ds is characterized by a porous structure with the dominance of mesopores (2–50 nm) and also including pores in the microporous region (<2 nm). The textural characteristics of the optimized hydrochar and activated hydrochar are presented in Table 3.

SampleSBET (m2/g)Vp (cm3/g)Vmicro (cm3/g)Vmeso (cm3/g)Dp (nm)


The hydrochar optimized under the conditions XA = 200°C, XB = 120 min, and XC = 20 mg is characterized by a BET surface area of 60.75 m2/g and a pore volume of 0.14 cm3/g. These results are similar to the results of [59] in the case of hazelnut shell and a little high compared to those reported by [39, 60] in the case of residues from the wine industry and salacca peel, respectively. This finding can be explained by the type of raw material and the conditions of synthesis, including the introduction of citric acid as a catalyst in the hydrothermal reaction. Indeed, our results are in agreement with those reported by [39, 40, 59], which showed the positive effect of acidic conditions in the hydrothermal reaction on the porous structure of the hydrochar. In contrast, the pore size distribution by the BJH method shown in Figure 4(b) shows that AOHC-Ds has a wide mesopore size distribution (2–50 nm) with a peak of 3 nm and 8.75 nm for OHC-Ds. Another interesting result is that the biomass/citric acid mass ratio used for the formation of OHC-Ds 2 : 0.1 is lower than 8 : 0.1 reported by [59] or 5 : 0.1 by [39], which is excellent from an economic point of view for pilot scale use. On the other hand, the BET surface area of the same hydrochar after AOHC-Ds activation is 1251.5 m2/g (Figure 4(a)), 20 times more than that of OHC-Ds. In addition, the total pore volume increased from 0.14 cm3/g to 0.736 cm3/g with a considerable increase in the mesopore volume from 0.12 cm3/g to 0.426 cm3/g, confirming the dominance of mesopores in the AOHC-Ds structure. In comparison, our results, which are slightly lower than those reported by [61] who have elaborated an activated carbon from the same precursor (with the conditions and textural characteristics relative to Table 7S), lead us to say that the preparation of a porous carbonaceous material from date seed by citric acid-catalyzed HTC followed by a chemical treatment proves to be more efficient than the application of HTC alone followed by a chemical or physical treatment.

3.3.3. FT-IR, XRD Analysis, and pHPZC

The FT-IR vibration spectra used to evaluate the effect of citric acid-catalyzed HTC on the surface functions of Ds, OHC-Ds, and AOHC-Ds are shown in Figure 5(a) and Table 8S. These spectra show eight zones suggesting the chemical structure and surface functional groups of these materials. First of all, the vibration spectrum of OHC-Ds is different from that of Ds, notably in the zone 1, a large bung at 3400 cm−1 which shows a medium narrowness attributed to the stretching hydroxyl (-OH) group present in the structure of cellulose and hemicellulose. This finding is due to dehydration, decarboxylation reactions, and hydrolysis, which took place during the HTC reaction of date seeds. These differences can be explained by the effect of temperature, which several authors have already shown [6163]. Then, the intensity of the bands was reduced in particular in the zone 4 to 1720 cm−1 at medium intensity, in the zone 7 to 1182 cm−1 at high intensity, and in the zone 8 to 1100 cm−1 at medium intensity, corresponding, respectively, to the elongation of the group (C=O) of the carboxylic acids, the elongation of the group (C-O) in the tertiary ester/alcohol (simple aliphatic), the elongation of the group (C-N), and the elongation of the group (O-H) of the alcohols [64]. These findings may be not only due to the temperature but also to the effect of citric acid. Recently, a study [39] showed that citric acid-catalyzed temperature increase in HTC to decrease the intensity of the (-OH), (-C-H), (C-O), and (C-O-H) grouping in the case of salacca peel. In this study, the decrease in the intensity of the vibrational bunches during citric acid-catalyzed HTC specifically for the date nucleus is due to the operating conditions (temperature and reaction time) and also favored by the contribution of citric acid to the dehydration, decarboxylation, and hydrolysis reactions. This decomposing nature of citric acid increases with the increasing amount added, consistent with the results found in van Krevelen diagram in Figure 3. On the other hand, the spectrum of AOHC-Ds shows a significant decrease relative to the hydrochar OHC-Ds in most bands except for the (-C-H) band at 2930 cm−1, (-C-H) alkanes at 2860 cm−1, (-CH) methyl group at 1450 cm−1, and (C=C) unsaturated α, β-ketone at 1620 cm−1 [65]. This is due to the chemical treatment with potassium hydroxide (KOH) followed by activation at 600°C. These functional groups are very important in the adsorption process, as they play the role of an active site capable of interacting with model molecules [66]. The effect of citric acid-catalyzed HTC on the crystal structure of OHC-Ds and AOHC-Ds was analyzed by X-ray diffraction (Figure 5(b)). As can be seen, the two XRD curves show that OHC-Ds and AOHC-Ds have an amorphous crystal structure. Obviously, the broad diffraction peak at 2θ = 26° is attributed to the (002) plane of the amorphous carbon comparable to graphite [67]. Indeed, the AOHC-Ds curve records another diffraction peak at 2θ = 43° less wide than the first one, attributed to the (100) plane, which indicates that the degree of graphitization increases with KOH treatment at 600°C, which is in agreement with the studies of [6870]. For the pH of AOHC-Ds at the zero-charge point shown in Figure 5(c), the curve pHinitial = f (pHfinal) intersection with the bisector reveals that the pHpzc of AOHC-Ds equals 6.75. This means that below pHpzc, the surface of AOHC-Ds is positive, promoting adsorption between AOHC-Ds and negatively charged molecules and vice-versa [71].

3.4. Adsorption Batch
3.4.1. Effect of the Adsorption Parameter on the Removal Rate

Figure 6 shows the evolution of MB and MO removal rate as a function of pH in the range of 2–12 with a 5 mg AOHC-Ds mass, an initial concentration set at 50 mg/L for both dyes for 4 hours. As can be seen, the R% increases with increasing pH for MB and contrary to MO. The high adsorbed amount for MB was obtained at pH = 8, and then, the amount remains unchanged. This can be explained by the competition between the ions (H+) in the acid region of pH 2–7 and the MB molecules for the vacant pore’s occupation on the surface of AOHC-Ds. In the basic pH, the electrostatic force becomes important, which increases the R(%). However, the optimal rate R(%) for MO has been obtained at pH = 5. This is due to the negative charge carried by the MO competing with the ions (-OH) in the basic region, which makes the R(%) less effective. In this context, we continued the adsorption tests by taking pH values of 8 and 5 for MB and MO, respectively. By varying the mass of AOHC-Ds from 2.5 mg to 25 mg (Figure 6(a)), it can be seen that the percentage of elimination R% increases up to 96%, corresponding to a mass of 0.01 g in the case of MB and then stabilizes despite the increase in the dose of AOHC-Ds. Similarly, for MB, the same variation is observed, with a maximum elimination rate of 70% at 0.01 g. Therefore, the maximum dose for both dyes is taken as 0.01 g. Several studies have reported that increasing the dose of adsorbent increases the elimination rate or the amount adsorbed [36, 72, 73]. Figure 6(c) shows that both dyes’ removal rate increases to a maximum and then degrade. This is due to the availability of vacant pores in the structure of AOHC-Ds, which fills entirely at the concentration of 500 mg/L for MB and 300 mg/L for MO. Indeed, our results are in perfect agreement with recent studies [74]. The results for the contact time shown in Figure 6(d) revealed that the removal rate of MB and MO increases rapidly and reaches its maximum in 10 min for MB and 25 min for MO.

3.4.2. Adsorption Isotherm

The two most widely used models, Langmuir and Freundlich, for evaluating MB and MO adsorption behavior on AOHC-Ds were studied. The parameters of these two models are given in Table 4. First, based on the value of the R2 coefficient, we find that the Langmuir model is closest to 1 for MB (0.83) and OM (0.89). On the one hand, this reveals that the Langmuir model better describes the adsorption process of MB and MO on AOHC-Ds than the Freundlich model. On the other hand, it reveals that the adsorption process probably occurs in a monolayer on the homogeneous surface of AOHC-Ds according to [75]. We also find that the coefficient R2 for the two isotherms in MB adsorption is very close, 0.83 for the Langmuir isotherm and 0.82 for Freundlich, indicating that both isotherms can describe the MB adsorption process. Next, the constant RL is between 0.012 and 0.29 for MB adsorption, and 0.0036–0.01 for MO indicates that the adsorption process of the two dyes MB and MO is favorable on the AOHC-Ds. In addition, the maximum adsorption capacity Qmax calculated by the Langmuir model is 657.89 (mg g−1) for MB and 384.61 (mg g−1) for MO. This high value of Qmax is due to two things: the better affinity of AOHC-Ds towards methylene blue molecules, which is in agreement with the isotherms calculated parameters, notably the KL value, which is less than 1. Then, there is the high specific surface area (1251.5 m2/g) and the pore volume (0.736 cm3/g) obtained with AOHC-Ds, which play a crucial role in the adsorption process [7]. From these results, the possible adsorption mechanisms are an electrostatic attraction, interactions π-π or n-π, in the case of MB adsorption according to [76] and the formation of the hydrogen bond and the hydrophobic interaction in the case of methyl orange [77].

Isothermal modelParametersBMOM

LangmuirQm (mg g−1)657.89384.62
KL (L mg−1)0.0980.329
RL range0.012–0.290.0036–0.0108

FreundlichKF (mg/g (1/mg))407.320265.49606

4. Comparison with Previous Work

Table 7S shows the maximum adsorption capacities (Qmax) of carbonaceous materials prepared from other precursors, agricultural by-products, and industrial wastes. It is quite clear that the synthesis condition plays a significant role in the formation of a porous material with moderate and controlled characteristics such as the specific surface area. Indeed, by comparing the adsorption capacities by the synthesis method proposed in this study with the one mentioned in Table 7S, we can say that the coupling of hydrothermal carbonization catalyzed by citric acid is efficient and less expensive for two reasons. First, the precursor used is an agricultural by-product considered waste, which means that its cost is lower than that used for the production of activated carbon such as wood. Second, the synthesized material AOHC-Ds has shown comparable efficiency compared to other raw materials in removing methylene blue and methyl orange. All these properties make our material very promising for the remediation of dye-contaminated water.

5. Conclusion

The application of citric acid-catalyzed hydrothermal carbonization in this study using the surface response methodology demonstrated its effectiveness in converting the date seeds to hydrochar. Under the conditions XA = 200°C, XB = 120 min, and XC = 20 mg, CHTC produced an optimized carbon-rich hydrochar. The activation of the optimized hydrochar gave a mesoporous material with interesting characteristics comparable to activated carbon. Characterizations by XRD, FTIR, and BET techniques show that our material is amorphous with a large specific surface area of 1251.5 m2/g and contains interesting functions on its surface, which allow it to be a good candidate in the field of adsorption. The methylene blue and methyl orange adsorption tests performed on AOHC-Ds showed a good adsorbent-adsorbate affinity represented by the maximum adsorption capacity of 657.89 mg g−1 for MB adsorption and 384.61 mg g−1 for MO adsorption. CHTC coupling and chemical activation followed by pyrolysis proposed in this study promise to produce porous carbon-rich materials derived from biomass and lignocellulosic wastes.

Data Availability

The data used to support the findings of this study are included within the article and in Supplementary Materials and are also available from the corresponding author upon request.

Conflicts of Interest

The authors declare that they have no conflicts of interest.

Supplementary Materials

Additional data related to this are included in the Supporting Information file. Figure 1S. Geometrical location of the experimental points of the CCD design for k = 3 factors and α = 1.68. Figure 2S. (a) 2D plot of the Ym(%) and (b) response surface of the Ym(%) with a fixed catalyst dose (XC = 17.5 mg). Figure 3S. (a) 2D plot of the CRR(%) and (b) response surface of the CRR(%) with a fixed reaction time (XB = 90 min). Figure 4S. (a) Bar histogram and (b) graphical representation of the desirability function for the optimal solution (D = 0.887). Table 1S. Experimental matrix of the CCD design. Table 2S. ANOVA analysis for the quadratic mass yield model. Table 3S. ANOVA analysis for the quadratic carbon recovery rate model. Table 4S. Optimization constraints. Table 5S. Elemental analysis, atomic ratios, and higher heating value HHV of hydrochars produced using the CCD design. Table 6S. Equations used in the calculation of MO and MB adsorption on AOHC-Ds. Table 7S. Comparison of adsorption performance of AOHC-Ds with other works. Table 8S. Group functional with their frequency wavenumber extracted from the FTIR analysis. (Supplementary Materials)


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