# Sustainable Removal of Basic Fuchsine and Methylene Blue Dyes Using Chicken Bone Biomass: Thermodynamics, Kinetics, and Insights from Experimental Studies and Decision Tree with Least Squares Boosting Predictive Modeling

Assia Ouzani, Yamina Zouambia, Hamida Maachou, Mohamed Krea, Aymen Amine Assadi, Lotfi Khezami, Yacine Benguerba, Jie Zhang, Abdeltif Amrane, Walid Elfalleh, et al.

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Assia Ouzani, Yamina Zouambia, Hamida Maachou, Mohamed Krea, Aymen Amine Assadi, et al. Sustainable Removal of Basic Fuchsine and Methylene Blue Dyes Using Chicken Bone Biomass: Thermodynamics, Kinetics, and Insights from Experimental Studies and Decision Tree with Least Squares Boosting Predictive Modeling. Water, 2025, 17 (7), pp.1053. 10.3390/w17071053. hal-05025084

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Article

# Sustainable Removal of Basic Fuchsine and Methylene Blue Dyes Using Chicken Bone Biomass: Thermodynamics, Kinetics, and Insights from Experimental Studies and Decision Tree with Least Squares Boosting Predictive Modeling

Assia Ouzani <fnref n="1" />, Yamina Zouambia <fnref n="1" />, Hamida Maachou <fnref n="1" />, Mohamed Krea <fnref n="1" />, Amine Aymen Assadi <fnref n="2" />,* ID,
Lotfi Khezami <fnref n="3" /> ID, Yacine Benguerba <fnref n="4" />, Jie Zhang <fnref n="5" /> ID, Abdeltif Amrane <fnref n="6" /> ID, Walid Elfalleh <fnref n="7" /> ID
and Hichem Tahraoui <fnref n="8" /> ID

<figure><img src="image_2.png" /></figure>

check for
updates

Academic Editor: Laura Bulgariu

Received: 6 February 2025

Revised: 29 March 2025

Accepted: 31 March 2025

Published: 2 April 2025

**Citation:** Ouzani, A.; Zouambia, Y.; Maachou, H.; Krea, M.; Assadi, A.A.; Khezami, L.; Benguerba, Y.; Zhang, J.; Amrane, A.; Elfalleh, W.; et al.
Sustainable Removal of Basic Fuchsine and Methylene Blue Dyes Using Chicken Bone Biomass: Thermodynamics, Kinetics, and Insights from Experimental Studies and Decision Tree with Least Squares Boosting Predictive Modeling.
*Water* **2025**, *17*, 1053. https://doi.org/10.3390/w17071053

**Copyright:** © 2025 by the authors.
Licensee MDPI, Basel, Switzerland.
This article is an open access article
distributed under the terms and
conditions of the Creative Commons
Attribution (CC BY) license
(https://creativecommons.org/
licenses/by/4.0/).

**Abstract:** This study addresses the dual challenges of water pollution and waste management by exploring the valorization of chicken bone biomass in native (NBio) and calcined (CBio) forms as biosorbents for dye removal. Basic fuchsine (BF) and methylene blue (MB) were selected as model pollutants, and adsorption was assessed under varying operational conditions. Characterization using Fourier-transform infrared spectroscopy (FTIR), scanning electron microscopy (SEM), and X-ray diffraction (XRD) showed that calcination improved crystallinity, eliminated organic impurities, and increased surface area (247 m<fnref n="2" />/g for NBio vs. 370 m<fnref n="2" />/g for CBio). Adsorption tests revealed higher performance for CBio, with maximum adsorption capacities of 100 mg/g (BF) and 142.85 mg/g (MB) based on the Langmuir isotherm, while NBio with maximum adsorption capacities of 111 mg/g (BF) and 111.11 mg/g (MB) followed the Freundlich model. Adsorption kinetics indicated pseudo-second-order behavior, suggesting chemisorption. The possible interactions between dyes and the biosorbent are hydrogen bonding, electrostatic interactions, and Lewis acid-base interactions. Thermodynamic analysis highlighted exothermic behavior for NBio and endothermic, entropy-driven adsorption for CBio, with both processes being spontaneous. A decision tree with Least Squares Boosting (DT_LSBOOST) provided accurate predictions (R<fnref n="2" /> = 0.9999, RMSE < 0.003) by integrating key parameters. These findings promote chicken bone biomass as a cost-effective, sustainable biosorbent, offering promising potential in wastewater treatment and environmental remediation.

**Keywords:** chicken bone biomass; biosorption; synthetic dyes; decision tree modeling; least squares boosting

<footnote n="1">¹ Laboratory Materials and Environment, University Yahia Fares of Medea, Urban Center, Medea 26000, Algeria</footnote>

<footnote n="2">² College of Engineering, Imam Mohammad Ibn Saud Islamic University (IMSIU), Riyadh 11432, Saudi Arabia</footnote>

<footnote n="3">³ Department of Chemistry, College of Science, Imam Mohammad Ibn Saud Islamic University (IMSIU),
Riyadh 11623, Saudi Arabia</footnote>

<footnote n="4">⁴ Laboratoire de Biopharmacie et Pharmacotechnie (LBPT), Ferhat Abbas Setif 1 University, Setif 19137, Algeria</footnote>

<footnote n="5">5 Université de Rennes, Ecole Nationale Supérieure de Chimie de Rennes, CNRS, ISCR-UMR6226,
F-35000 Rennes, France</footnote>

<footnote n="6">6 School of Chemical Engineering and Advanced Materials, Newcastle University,
Newcastle upon Tyne NE1 7RU, UK; abdeltif.amrane@univ-rennes.fr</footnote>

<footnote n="7">⁷ Department of Biology, College of Science, Imam Mohammad Ibn Saud Islamic University (IMSIU),
Riyadh 11623, Saudi Arabia; elfallehwalid@gmail.com</footnote>

<footnote n="8">8 Laboratory of Biomaterials and Transport Phenomena (LBMTP), University Yahia Fares of Medea,
Medea 26000, Algeria; tahraoui.hichem@univ-medea.dz</footnote>

<footnote>* Correspondence: aaassadi@imamu.edu.sa; Tel.: +966-563260210</footnote>
# 1. Introduction

The increasing demand for freshwater resources is a critical global challenge, as highlighted in the 2021 World Water Development Report published by UNESCO. This report reveals that global freshwater usage has surged sixfold over the past century and continues to grow at an approximate annual rate of 1% since the 1980s [1,2]. Although water is abundant on Earth's surface, only a small fraction is freshwater, accounting for merely 2.6%, with less than 1% being directly accessible for human consumption and other uses; the majority exists in the form of glaciers and ice caps [3,4]. This limited availability underscores the urgent need for sustainable water management, particularly given the extensive use of freshwater by various industries such as textiles, tanning, paper manufacturing, plastics, and dye production [5,6].

Industrialization, coupled with rapid urbanization and a lack of environmental awareness, has led to the widespread discharge of untreated industrial effluents, hazardous chemicals, and other pollutants into natural water bodies [4]. Such practices have significantly degraded freshwater resources, rendering them unsuitable for consumption or other applications. Statistics indicate that approximately 80% of wastewater, originating from both industrial and urban activities, is released into the environment without undergoing any form of treatment [7]. This issue is especially pronounced in developing countries, where the lack of wastewater treatment infrastructure and sanitation facilities exacerbates the problem. Untreated wastewater is a major environmental concern as it introduces toxic and persistent pollutants into ecosystems, posing serious risks to both human health and biodiversity [8–10].

One of the most significant contributors to water pollution is synthetic dyes, extensively utilized in numerous industries for coloring textiles, plastics, papers, and other materials [10]. Between 2016 and 2023, the dye industry, dominated by Asia, experienced substantial growth, with an estimated annual increase of 8.13% [11]. Among the industrial sectors, the textile industry is responsible for the largest share of dye pollution, releasing approximately 54% of all dye effluents into the environment. These pollutants cause a range of environmental issues, such as the discoloration of water, a reduction in dissolved oxygen levels, and the destruction of aquatic ecosystems, which negatively impact flora and fauna [12]. As a result, it is essential to implement effective treatment methods to remove dyes from wastewater before discharge.

Numerous methods have been developed to address dye contamination in water, including advanced physicochemical techniques such as coagulation [13], advanced oxidation [14–16], microalgae [17], and membrane filtration [18–21]. While these methods are effective in certain contexts, they often face limitations such as high operational costs, the generation of secondary pollutants, and a reliance on potentially hazardous chemicals. This has led researchers to focus on alternative remediation approaches that are environmentally friendly, cost-effective, and free from undesirable side effects.

Among these approaches, adsorption has emerged as a highly promising technique for dye removal due to its simplicity, efficiency, and adaptability [22]. The effectiveness of an adsorption process depends largely on the properties of the adsorbent material, including its mechanical stability, selectivity for specific pollutants, adsorption capacity, cost of regeneration, and environmental compatibility [23]. Therefore, adsorption technologies have gained widespread attention as an effective solution for wastewater treatment due to their high capability to remove organic and inorganic pollutants from aquatic environments. Sustainable adsorbent materials, such as activated carbon and nanocomposites, are promising alternatives to conventional techniques due to their efficiency, ease of use, and potential for regeneration and reuse [24]. Moreover, recycling solid waste to produce adsorptive materials enhances environmental sustainability by reducing industrial
and agricultural waste while providing cost-effective solutions for treating contaminated water [25]. Among the promising applications, hybrid materials, such as nanomaterials supported by activated carbon, have emerged as effective adsorbents for removing various pollutants from wastewater. These materials enhance adsorption efficiency by increasing the specific area and improving the physicochemical properties of the adsorbent [26]. These advancements highlight the importance of continuous research in optimizing adsorption technologies and solid waste recycling to develop more efficient and sustainable solutions for wastewater treatment. In recent years, there has been growing interest in the use of low-cost, eco-friendly adsorbents derived from agricultural and industrial waste. Examples of such materials include potato peel [27], apple peel [28], orange peel [29], coffee waste [30], wheat husk [31], and loofah cylindrica [21]. These biomaterials offer dual benefits: they provide an efficient solution for wastewater treatment while also addressing the issue of waste management [30–35].

In Algeria, a significant amount of animal bones is generated as waste from the food industry [35–40]. These bones are often discarded, contributing to environmental pollution. However, their abundance and natural composition make them a viable candidate for valorization as biosorbents in wastewater treatment [41–44]. Utilizing these waste materials aligns with the principles of sustainability, as it promotes resource recovery and environmental protection [45–48]. It has two benefits: it addresses the rising issue of wastewater tainted with dyes and offers a useful recycling solution for poultry waste, which would otherwise contribute to environmental pollution [48–52]. Furthermore, its low cost, availability, and eco-friendly nature make it an attractive alternative to synthetic adsorbents, promising an efficient and sustainable approach to wastewater treatment.

Traditional modeling approaches for adsorption process optimization often rely on empirical equations and linear regression models [32]. While these techniques provide valuable insights, they may struggle to capture complex, nonlinear interactions between multiple adsorption parameters. Moreover, their predictive accuracy is often limited when dealing with large datasets or diverse experimental conditions exhibiting nonlinear relationships [32]. Machine learning (ML) and artificial intelligence (AI) techniques have emerged as powerful alternatives, offering enhanced predictive capabilities by learning nonlinear relationships from experimental data [32].

Among AI-based models, decision trees (DTs) have gained attention due to their ability to handle nonlinear relationships and provide interpretable models [33,34]. A DT is a supervised learning model that segments data based on successive criteria, forming a hierarchical structure [33,34]. Each internal node of the tree represents a rule or condition on a specific data feature, while each leaf corresponds to a final prediction or class. Despite their advantages, decision trees can be prone to overfitting, particularly when applied to noisy datasets or highly complex systems, and they may struggle to fully capture intricate interactions between adsorption parameters [33,34].

To overcome these limitations, ensemble learning techniques such as Least Squares Boosting (LSBOOST) have been introduced [33,34]. LSBOOST is an iterative boosting algorithm that combines the predictions of multiple weak models to generate a robust final model. Unlike traditional ensemble methods, LSBOOST corrects errors at each iteration, improving predictive accuracy and reducing overfitting. By integrating LSBOOST with decision trees (DT_LSBOOST), it is possible to enhance the accuracy and reliability of adsorption process modeling, effectively capturing both linear and nonlinear interactions while maintaining model interpretability [33,34].

In this work, an in-depth study was conducted to evaluate the potential of chicken biomass as a sustainable biosorbent for the treatment of water contaminated with synthetic dyes. Two distinct forms of biomass were prepared: a native form and a calcined form,
obtained by high-temperature thermal treatment. The work began with the preparation of the biosorbents, including meticulous cleaning, grinding, and controlled calcination to remove organic impurities and modify the structure of the biomass. These samples were then characterized using techniques such as Fourier-transform infrared spectroscopy (FTIR), scanning electron microscopy (SEM), and X-ray diffraction (XRD), allowing the documentation of their structural and morphological properties. The specific surface area of the biosorbents was also determined using a method based on methylene blue adsorption. A comprehensive experimental study was carried out to evaluate the adsorption performance of both biosorbents with respect to two dyes, basic fuchsine and methylene blue. The effects of several operational parameters, including contact time, initial dye concentration, and adsorbent mass, were examined to understand the underlying adsorption mechanisms. The data obtained were analyzed using kinetic models (pseudo-first order, pseudo-second order, and intra-particle diffusion) to explore the adsorption kinetics mechanisms. Additionally, Langmuir and Freundlich adsorption isotherms were fitted to the experimental data to describe the adsorbent-adsorbate interactions and characterize the adsorption capacities at equilibrium. A thermodynamic analysis was also conducted to determine the spontaneity and the energetic nature of the adsorption processes. Additionally, a predictive model based on a coupling of a decision tree and a Least Squares Boosting method (DT_LSBOOST) was developed. This model allows the prediction of adsorption capacities based on experimental parameters, integrating continuous variables (time, concentration, and mass) and categorical variables (dye type and biosorbent type). Finally, a MATLAB R2022b application was developed to facilitate the prediction of biosorbent adsorption capacities based on experimental parameters. This application utilized the DT_LSBOOST model, allowing researchers to simulate different adsorption conditions and obtain reliable predictive results, thereby contributing to the optimization of the water treatment process. This comprehensive approach enabled the understanding of the biosorbents' properties and the optimization of their use for dye adsorption under varying conditions, while also proposing an innovative predictive methodology for future applications.

This study presents a novel approach to valorizing chicken bone biomass, emphasizing its potential as a sustainable and efficient biosorbent for wastewater treatment. By exploring both (NBio) and (CBio) forms, it provides a comprehensive understanding of how thermal treatment enhances adsorption performance. The dual-state comparison is a key innovation, shedding light on the structural, morphological, and functional transformations induced by calcination. The research employs characterization techniques, including FTIR, SEM, XRD, and specific surface area analysis, to investigate the changes in properties of the biosorbents. These analyses reveal how calcination impacts the surface area, crystallinity, and porosity, offering detailed insights into the mechanisms underlying improved adsorption capacity. This thorough structural assessment is a critical step forward in understanding and optimizing biosorbent performance. A significant contribution of this study lies in its integration of experimental and predictive modeling methodologies. Adsorption kinetics and equilibrium studies are coupled with thermodynamic analyses, offering a holistic view of the biosorption process. The kinetic models help identify the dominant adsorption mechanisms, while thermodynamic evaluations provide insights into the energy dynamics and feasibility of the process under various conditions. Additionally, a predictive modeling application was developed using a decision tree coupled with Least Squares Boosting (DT_LSBOOST) to estimate adsorption capacities with exceptional accuracy. This MATLAB-based application allows users to input key experimental parameters, including contact time, adsorbent dosage, dye concentration, and the type of dye and biosorbent, to instantly predict adsorption outcomes. This application bridges the gap between research and practical implementation, providing a user-friendly tool for optimizing wastewater
treatment processes. Finally, this research aligns with sustainability principles by repurpos-
ing a widely available food industry byproduct into an effective solution for environmental
remediation. By transforming waste materials into high-performance adsorbents, this study
addresses critical challenges in pollution control and resource recovery, offering a scalable
and environmentally friendly approach to tackling water pollution.

## 2. Materials and Methods

### 2.1. Adsorbate

MB is a synthetic dye prepared via the oxidation reaction of 4-aminodimethylaniline in the presence of sodium thiosulfate. It has many potential applications in the textile, pharmaceutical, paper, dyeing, printing, paint, medicine, and food industries [35]. Basic fuchsin, also known as basic violet 14, is a cationic dye commonly used for coloring biological tissues and textiles [36]. The toxicity limits of colorants such as methylene blue and fuchsin basic dye are regulated according to environmental and health standards that vary from country to country and region to region. Discharge limits vary according to local legislation; for example, the U.S. Environmental Protection Agency (EPA) recommends concentration levels in wastewater below 1 mg/L to prevent environmental impacts [37].

BF and MB, used in this study, were of analytical grade basic dyes with 95% purity and were purchased from Sigma-Aldrich (Burlington, MA, USA).

### 2.2. Preparation of Adsorbents

In this study, two biomass samples derived from chicken bones were prepared following a specific procedure. Initially, any remaining meat and fat were removed through combustion using a blowtorch. The bones were then cleaned with distilled water, dried in an oven, and ground into a fine powder using a mortar. The resulting powder, with a particle size of 250 µm, was labeled as NBio. To produce the second sample, named CBio, the NBio powder was subjected to a thermal treatment at 900 °C in a Nabertherm muffle furnace.

### 2.3. Characterization of the Biomass Adsorbents

FTIR was employed using a Vertex 70 spectrophotometer (Bruker, Billerica, MA, USA) to identify the functional groups present in the biomass adsorbents. The spectral data were collected over a range of 4000–400 cm⁻¹, with a resolution of 8 cm⁻¹, and averaged across 128 scans to ensure precise results. The structural morphology of NBio and CBio was analyzed through SEM to visualize their surface characteristics. Furthermore, XRD analysis was carried out using an X-ray powder diffractometer to investigate the crystallographic parameters and evaluate the phase purity of the biosorbents. This analysis utilized monochromatic copper Kα radiation (λ = 1.5406 Å), with the diffraction angle (2θ) scanned between 5° and 100° at increments of 0.026°. The lattice constant parameters (a = b and c) were determined using Equation (1) as outlined by Kumar et al. [38].

$$ \frac{1}{d^2} = \frac{4}{3} \left[ \frac{h^2 + k^2 + hk}{a^2} \right] + \frac{l^2}{c^2} \quad (1) $$

The crystallite size of the biosorbents was calculated by Debye–Scherrer’s equation (Equation (2)) [39].

$$ D_h = \frac{k\lambda}{\beta \cos \theta} \quad (2) $$
## 2.4. Determination of Specific Surface Area

The specific surface area of the two biosorbents was determined based on the MB biosorption data, as previously described by Bencheikh et al. [40]. This approach involves the adsorption of MB molecules by a specified amount of biosorbent from MB solutions with varying concentrations until equilibrium is reached. At equilibrium, the MB molecules are adsorbed and form a monolayer on the biosorbent surface. In this study, adsorption was carried out by combining 0.1 g of NBio or CBio with MB solutions ranging from 10 to 100 µM. The mixture was stirred at 250 rpm at room temperature, and the MB concentration was measured at various time intervals until equilibrium was attained, using a UV-visible spectrophotometer (Shimadzu UV-1800, Kyoto, Japan). The maximum amount of MB adsorbed was then used in Equation (3) to calculate the specific surface area (A) of the biosorbent:

$$A = \frac{b * N * A_{MB}}{M} \qquad (3)$$

## 2.5. Adsorption Study

The effect of contact time on the biosorption capacities of BF and MB by NBio and CBio was evaluated using an initial dye concentration of 10 mg L⁻¹, a solution volume of 50 mL, and 0.05 g of adsorbent, all maintained at room temperature. The final concentrations of BF and MB were measured at different time points (ranging from 3 to 70 min) using a UV-visible spectrophotometer at 574 nm and 676 nm, respectively. To investigate the influence of initial dye concentration on the biosorption capacity, the concentration was adjusted between 20 and 140 mg L⁻¹ in increments of 20 mg L⁻¹. The effect of the adsorbent mass was studied within the range of 0.015 to 0.25 g, with an initial dye concentration of 10 mg L⁻¹, a dye solution volume of 50 mL, and no pH adjustment. The effect of the biosorbent/adsorbate ratio was examined by varying the amounts of NBio (0.01–0.15 g) or CBio (0.01–0.25 g), while keeping the dye volume and concentration constant. The adsorption capacities, Qe (mg g⁻¹), for BF and MB on NBio and CBio were calculated using Equation (4).

$$Q_e = \frac{C_i - C_e}{m} * V \qquad (4)$$

## 2.6. Kinetic Study

In this study, the adsorption kinetics were analyzed through the application of three different models: the pseudo-first-order, pseudo-second-order, and intra-particle diffusion models. These models were selected based on their relevance in describing the dynamics of solute removal during the adsorption process.

### 2.6.1. Adsorption Kinetic Models

The pseudo-first-order kinetic model, originally proposed by Lagergren in 1898, is one of the most commonly used models for describing the adsorption process at low solute concentrations [41]. According to Bessashia et al. [41], this model is particularly effective when the concentration of the adsorbate is relatively low. It assumes that the rate of adsorption is proportional to the difference between the equilibrium concentration and the concentration at a given time, leading to a linear relationship that can be used to estimate the rate constant.

The linearized form of the Lagergren pseudo-first-order model can be expressed by Equation (5), which allows for the determination of the adsorption rate constant based on experimental data. This model is widely utilized in environmental engineering and
material science to describe adsorption processes such as the removal of contaminants from water or air by various adsorbents.

$$ \log(Q_e - Q_t) = \log Q_e - \frac{K_1}{2.303} t \qquad (5) $$

The pseudo-second-order kinetic model is based on the assumption that the rate of adsorption is dependent on the concentration of the adsorbate and the availability of adsorption sites. This model accounts for two different types of adsorption processes: the fast adsorption of solutes onto the highly reactive sites of the adsorbent and the slower adsorption onto the less reactive, lower-energy sites. This dual mechanism allows the pseudo-second-order model to provide a more accurate description of adsorption processes, particularly when the adsorption rate decreases as the number of available sites becomes limited. The linearized form of the pseudo-second-order model, represented by Equation (6), enables the calculation of the adsorption rate constant and the amount of solute adsorbed at equilibrium. This model is particularly useful for describing adsorption systems where the rate of adsorption does not solely depend on the concentration of the solute but is also influenced by the availability of specific adsorption sites with varying affinities. The pseudo-second-order model is frequently applied in the study of adsorption phenomena in environmental and industrial processes, where the adsorption of pollutants, such as dyes or heavy metals, follows a two-stage process involving both rapid and slow adsorption phases.

$$ \frac{t}{Q_t} = \frac{1}{K_2 Q_e^2} + \frac{1}{Q_e} t \qquad (6) $$

Finally, the diffusion mechanisms governing the adsorption process were explored using the intra-particle diffusion model, also known as the Weber-Morris model, as detailed by Adeogun et al. [43]. This model is used to describe the movement of solute molecules within the pores of the adsorbent material during the adsorption process. According to the Weber-Morris model, the rate of diffusion is influenced by factors such as the size of the pores, the adsorption capacity of the adsorbent, and the concentration gradient between the adsorbate and the adsorbent surface. The model assumes that the adsorption occurs in multiple stages, with the initial rapid adsorption phase being followed by a slower diffusion phase as the solute molecules move deeper into the adsorbent material. The Weber-Morris model is represented by Equation (7), which helps in evaluating the rate of diffusion within the adsorbent's pores [44]. This model is commonly used to assess the effectiveness of adsorbents in various applications, such as water and wastewater treatment, where the rate of solute diffusion plays a critical role in determining the overall adsorption efficiency.

$$ Q_t = K_{id} * t^{\frac{1}{2}} + C \qquad (7) $$

The relationship between the adsorbate concentration in the liquid phase ($C_e$) and the equilibrium adsorbed amount ($Q_e$) is described by the Langmuir and Freundlich adsorption isotherms. The linearized forms of these two models are given by Equations (8) and (10), respectively.

### 2.6.2. Adsorption Isotherms

In the Langmuir model, adsorption occurs in such a way that the adsorbate molecules form a single layer on the surface of the adsorbent. This model assumes that all adsorption sites on the surface of the adsorbent are identical, meaning each site has the same affinity for the adsorbate molecules [45]. Furthermore, it posits that once an adsorbate molecule occupies a site, no further adsorption can take place at that particular site, as it becomes “saturated”. Thus, the Langmuir model describes a finite number of adsorption sites with a
fixed capacity, where each site can hold only one molecule of the adsorbate, leading to the formation of a monolayer.

This model also assumes that the process of adsorption is reversible and that there is no interaction between the adsorbed molecules. The linearized form of the Langmuir isotherm, expressed in Equation (8), allows for the determination of key parameters such as the maximum adsorption capacity and the affinity between the adsorbate and the adsorbent. This model is commonly applied in scenarios where the adsorption sites are uniform, and the adsorption process follows these idealized assumptions.

$$ \frac{1}{Q_e} = \frac{1}{(bQ_m)} * \frac{1}{C_e} + \frac{1}{Q_m} \quad (8) $$

The dimensionless separation factor ($R_L$), expressed in Equation (9), provides insight into the feasibility of the adsorption process. The nature of adsorption can be described as unfavorable when $R_L > 1$, linear when $R_L = 1$, favorable when $0 < R_L < 1$, or irreversible when $R_L = 0$ [46].

$$ R_L = \frac{1}{1 + K_L C_0} \quad (9) $$

The Freundlich isotherm is an empirical equation based on an exponential distribution of adsorption sites and energies [47]. Generally, to describe the equilibrium equation, we apply the linear formulae given by Equation (10).

$$ \ln Q_e = K_f + \frac{1}{n} \ln C_e \quad (10) $$

The Freundlich model is determined by plotting $\ln Q_e$ against $\ln C_e$. When (1/n) equals 1, the adsorption is linear, suggesting the presence of uniform adsorption sites and no interaction between the adsorbed molecules. When (1/n) is less than 1, additional adsorption sites appear, improving the adsorption capacity, and the process becomes favorable and chemical in nature. Conversely, when (1/n) is greater than 1, the adsorption is unfavorable, as the adsorption capacity decreases due to weaker bonding [48–50].

### 2.6.3. Thermodynamic Study

To assess whether the adsorption of MB and BF onto native and calcined biomasses occurs spontaneously, the biosorption process was carried out at various temperatures. The thermodynamic parameters, including free energy change ($\Delta G$), enthalpy change ($\Delta H$), and entropy change ($\Delta S$), were evaluated using the Van't Hoff equation. The relationship between the equilibrium constant ($K_d$) and temperature (T) was determined by plotting the natural logarithm of $K_d$ against the reciprocal of the temperature (1/T). These thermodynamic parameters provide insights into the nature of the adsorption process, including its spontaneity, the heat involved, and the disorder or randomness associated with the process. The Van't Hoff equation, Equation (11), was applied to calculate these values and further understand the thermodynamic feasibility of the biosorption process [51].

$$ \ln(K_d) = -\frac{\Delta H}{RT} + \frac{\Delta S}{R} \quad (11) $$

$$ \Delta G = -RT \ln (K_d) \quad (12) $$

### 2.7. Decision Tree Coupled with Least Squares Boosting

A DT is a supervised model that segments data into a hierarchical structure, valued for its simplicity and interpretability. However, it is prone to overfitting and struggles to capture complex relationships [33,34]. Integrating LSBOOST, a boosting algorithm,
addresses these limitations by combining multiple weak models to enhance prediction accuracy and robustness [33,34]. LSBOOST iteratively corrects errors, and its outputs serve as the foundation for a decision tree, ensuring both high performance and interpretability. This hybrid approach reduces bias and variance, effectively handles noisy or imbalanced data, and applies to various fields requiring both precision and transparency [33,34].

In this study, DT_LSBOOST was used to predict the adsorption capacity of NBio and CBio chicken biochars for the removal of MB and BF dyes. The adsorption process was modeled using critical experimental parameters: contact time (X1), adsorbent mass (X2), and dye concentration (X3) as input variables, while the adsorption capacity served as the output. To make the model broadly applicable to both adsorbents and dyes, two additional categorical inputs were included. The type of adsorbent (X4) was coded as "1" for CBio and "2" for NBio, and the type of dye (X5) was similarly coded as "1" for MB and "2" for BF. These adjustments allowed the model to integrate differences in adsorbent properties and dye behavior into a unified predictive framework.

The dataset was preprocessed by normalizing all variables to the range [-1, 1]. This normalization step ensured that the variables were on the same scale, reducing the risk of any single variable dominating the training process. Once normalized, the dataset was divided into three subsets: 70% for training, 15% for validation, and 15% for testing. The training set was used to construct the model, while the validation set was employed for tuning hyperparameters, preventing overfitting. The unseen test set was reserved for the final evaluation of the model to ensure an unbiased assessment of its performance on unseen data.

To achieve an optimal model, several hyperparameters of both the decision tree and LSBoost were carefully tuned. For the decision tree, parameters such as the Minimum Leaf Size, the maximum number of splits, the Minimum Parent Size, and the use of Surrogate splits were adjusted to balance model complexity and interpretability. LSBoost parameters, including the Number of Learning Cycles, the learning rate, and the number of variables sampled per split, were optimized to enhance the model's ability to iteratively reduce residual errors. The learning rate, set at 0.1, ensured gradual updates that balanced the convergence speed and stability [32].

The performance of the final model was assessed using two key metrics: the coefficient of correlation (R) and the root mean square error (RMSE) [52,53]. R provided a measure of how well the model explained the variance in the adsorption capacity, while RMSE quantified the average error between predicted and observed values.

# 3. Results and Discussion

## 3.1. XRD Analysis of Native and Calcined Biomasses

The XRD analysis of the NBio and CBio samples is presented in Figure 1, providing valuable insight into the crystallographic structure of both the native and calcined biomasses. The diffractogram of the NBio shown in Figure 1a reveals a broad peak at 19.8°, which can be associated with the amorphous phase of the sample. Additionally, two broad peaks are observed at 25.9° and 32.22°, which correspond to the (002) and (211) planes, respectively, as previously reported for hydroxyapatite (HAP) (JCPDS cards for XRD analysis) [54]. These peaks are characteristic of hydroxyapatite's crystalline structure, albeit in a less defined form due to the presence of amorphous materials in the native biomass. The peak at 29.22° further indicates the presence of calcite, suggesting that the native biomass contains a mixture of mineral phases.
<figure><img src="image_3.png" /><figcaption>**Figure 1.** XRD pattern of NBio (a) and CBio (b).</figcaption></figure>

In contrast, the XRD pattern of the CBio presented in Figure 1b displays several sharp and intense peaks, indicating a significant change in crystallinity after calcination. The peaks observed at 10.1°, 26°, 28.98°, 31.8°, 32.9°, 39.7°, 46.75°, and 49.96° correspond to specific Miller indices: (100), (002), (210), (211), (300), (310), (222), and (213), as listed in JCPDS card No. 00-009-0432. These peaks reflect the well-ordered crystalline structure that forms after the calcination of the native biomass. The difference in the sharpness and intensity of the peaks between NBio and CBio suggests that calcination enhances the crystallinity of the material, reducing the number of amorphous components and improving the overall order of the crystal lattice.

This improvement in crystallinity is further highlighted by the pronounced triplet between 31° and 33°, which becomes more distinct in the CBio sample, indicating that the material is more crystalline after calcination. This result supports the hypothesis that calcination leads to the decomposition of organic matter and the reorganization of
inorganic phases, leading to the formation of a more crystalline structure, similar to that of hydroxyapatite.

The lattice constant parameters, denoted as a, b, and c, were calculated from the XRD data using Equation (1). These values provide information on the dimensions of the unit cell and the overall symmetry of the crystal structure. The average crystallite size of both NBio and CBio was estimated using Scherrer's formula (Equation (2)), which allows for the determination of the size of the crystalline domains based on the width of the XRD peaks. The results, summarized in Table 1, show that the crystallite size increases significantly after calcination, from 38.6 nm for NBio to 54.76 nm for CBio. This increase in crystallite size indicates that calcination promotes the growth of the crystalline domains, bringing the size closer to that of standard hydroxyapatite (HAP), which has a crystallite size of 68.84 nm. This trend highlights the effect of calcination in improving the crystallinity and structural integrity of the biomass-derived material, making it more suitable for applications that require well-defined crystalline structures, such as in adsorption processes or biomaterial synthesis.

<table><caption>**Table 1.** Biomass parameters determined from XRD patterns compared to standard HAP.</caption><thead><tr><th>Parameter</th><th>HAP</th><th>NBio</th><th>CBio</th></tr></thead><tbody><tr><td>Lattice constant parameters (a, b, and c/Å)</td><td>a = b = 9.42<br>c = 6.88</td><td>a = b = 9.09<br>c = 6.89</td><td>a = b = 9.72<br>c = 6.89</td></tr><tr><td>Crystallite size (D<sub>n</sub>/nm)</td><td>68.84</td><td>38.69</td><td>54.76</td></tr></tbody></table>

## 3.2. FTIR Characterization

The infrared spectra of native and calcined chicken bone, shown in Figure 2, clearly exhibit the effects of heat treatment, which causes significant changes in the material's composition. The primary difference between the two spectra lies in the removal of organic compounds such as fats and proteins during calcination, as a result of the high temperature.

<figure><img src="image_4.png" /><figcaption>**Figure 2.** FTIR spectra of native biomass (blue) and calcined biomass (red).</figcaption></figure>

In the spectrum of the NBio, shown in Figure 2 (in blue), a broad band near 3278.33 cm⁻¹ is observed, corresponding to the stretching vibrations of hydroxyl (O-H) and amine (N-H) groups. This band is characteristic of the presence of moisture and certain functional groups in the organic matrix of the bone. The bands at 2922.18 cm⁻¹ and
2853.51 cm⁻¹ are due to the C-H stretching vibrations of the alkyl groups (CH₃ and CH₂), which are associated with the fats present in the native biomass. These fatty acids and other lipids are part of the organic content of the chicken bone before calcination. The peak at 1458.24 cm⁻¹ is related to the C-H deformation vibrations of the CH₃ groups, along with the C-O stretching of the carbonate groups [55], further indicating the presence of organic and mineral components in the native bone.

Additionally, the peaks at 1741.85 cm⁻¹ and 1538.08 cm⁻¹ are associated with the carboxyl (C=O) and amide (N-H) groups, which are typical of proteins and fats found in the native chicken bone. These peaks suggest the presence of proteinaceous material, such as collagen, and fat molecules. The peak at 1637.02 cm⁻¹ is due to the bending vibrations of water molecules that are physically adsorbed onto the surface of the bone. The 1163.33 cm⁻¹ peak corresponds to the C-N stretching vibrations of amines or amides, further supporting the presence of proteins in the native bone. Finally, the peaks at 1024.71 cm⁻¹ and 555.15 cm⁻¹ are attributed to the P-O bond vibrations of the phosphate groups [22], which are representative of hydroxyapatite (HAP), a major inorganic mineral component of bone. These peaks confirm the bone's mineral content, which is primarily composed of HAP.

After calcination, the spectrum of the CBio shows a significant transformation, as can be seen from Figure 2 (in red). The intense peaks at 1021.81 cm⁻¹, 598.98 cm⁻¹, and 561.60 cm⁻¹ correspond to the P-O bond vibrations in phosphate groups (PO₄³⁻), which are indicative of the preservation of the mineral phase after heat treatment. These peaks are similar to those found in the hydroxyapatite structure, demonstrating that calcination has maintained the mineral composition of the bone, despite the removal of the organic components.

The absence of the other peaks observed in the NBio spectrum, such as those related to the C-H, C-N, and carboxyl groups, strongly suggests that calcination has effectively decomposed the organic matter, including fats, proteins, and other volatile compounds. This removal process is essential for producing a more crystalline form of the bone's inorganic components, leaving behind a highly mineralized structure primarily composed of HAP. Therefore, the calcination process not only removes organic impurities but also enhances the crystallinity of the mineral phase, as confirmed by the more defined and intense peaks in the CBio spectrum.

The infrared spectra highlight the significant structural and compositional changes that occur when chicken bone undergoes calcination. The heat treatment removes most organic matter, resulting in a cleaner, more crystalline mineral structure, while preserving the fundamental phosphate-based mineral content.

### 3.3. SEM Characterization

The surface properties of the biomass, both before and after thermal treatment, were carefully analyzed using SEM. Figure 3 provides SEM images of both the NBio and the CBio, captured at a magnification of 2.00 kx after a heat treatment at 900 °C for 3 h. The SEM images clearly demonstrate that the surface morphology of the biomass undergoes a significant transformation following thermal treatment.

In the case of the NBio (Figure 3a), the surface appears dense and agglomerated, with a smooth, non-porous texture. The homogeneous nature of the NBio suggests a compact structure with minimal surface irregularities or voids. This surface structure is characteristic of a biomass sample before any high-temperature treatment, where organic matter remains intact, and the biomass does not exhibit significant crystallinity or porosity.
<figure><img src="image_5.png" /><figcaption>**Figure 3.** SEM micrographs of native (a) and calcined (b) biomasses.</figcaption></figure>

Conversely, the SEM image of CBio (Figure 3b) shows a markedly different morphology. The surface of CBio is irregular, with a noticeable rough texture and increased porosity. The calcined biomass underwent substantial structural changes due to the high-temperature treatment. This rougher and more irregular surface can be attributed to the thermal decomposition of organic materials, such as fats and proteins, during calcination, leaving behind a more crystalline and porous structure. The increased porosity of the small agglomerates in the CBio also suggests a significant transformation in the biomass's internal structure, likely leading to more available surface area for adsorption processes.

These findings are consistent with the XRD analysis, which revealed a higher degree of crystallinity in CBio compared to NBio. The increase in crystallinity is linked to the removal of amorphous organic components and the formation of a more defined crystalline structure under high-temperature conditions. The enhanced porosity and roughness of CBio, as observed in the SEM images, suggest that the thermal treatment not only enhances the crystallinity but also significantly alters the surface texture, which can be beneficial for various applications, such as adsorption processes.

### 3.4. Specific Surface Area

Table 2 provides a detailed summary of the specific surface area (A) values of the two biosorbents utilized in this study, as well as the values for other adsorbents reported in the previous literature. A significant increase in the specific surface area of the NBio was observed after subjecting it to thermal treatment at 900 °C, which is consistent with the changes in surface morphology identified earlier. Specifically, the surface area of the CBio was found to be 370 m² g⁻¹, which is notably higher than that of the NBio at 247 m² g⁻¹. This increase in surface area suggests a substantial alteration in the biomass structure due to calcination, contributing to enhanced adsorption properties.
<table><caption>**Table 2.** Specific surface areas (SMB) of native and calcined biosorbents, as well as other adsorbents from the literature.</caption><thead><tr><td>Adsorbents</td><td>S<sub>MB</sub>/m<sup>2</sup> g<sup>-1</sup></td><td>Reference</td></tr></thead><tbody><tr><td>NBio</td><td>247</td><td>This study</td></tr><tr><td>CBio</td><td>370</td><td>This study</td></tr><tr><td>Bone Char</td><td>113–119</td><td>[56]</td></tr><tr><td>Kaïcedra</td><td>39.40</td><td>[57]</td></tr><tr><td>Pin</td><td>79.65</td><td>[57]</td></tr><tr><td>Bioadsorbent from agricultural waste of Cucumeropsis mannii Naudin</td><td>252</td><td>[49]</td></tr></tbody></table>

Furthermore, when compared to other adsorbents mentioned in the literature, the surface area of NBio (247 m² g⁻¹) was found to be comparable to that of a bioadsorbent derived from the agricultural waste of Cucumeropsis mannii Naudin (252 m² g⁻¹), as reported by Kifuani et al. [49]. This indicates that the thermal treatment applied in this study significantly enhances the adsorptive capacity of the biomass, bringing it on par with other bioadsorbents that have been successfully used in similar applications. The increased surface area can be attributed to the removal of organic components during calcination, resulting in a more crystalline and porous structure that is better suited for adsorbing contaminants, as observed from both the surface morphology and surface area analysis.

### 3.5. *Parametric Study*

#### 3.5.1. Effect of Contact Time

The adsorption kinetics shown in Figure 4 can be divided into three distinct phases, each representing a different rate of adsorption and providing insights into the interaction between the adsorbate and the biosorbent.

<figure><img src="image_6.png" /><figcaption>**Figure 4.** Impact of the contact time on BF (a) and MB (b) biosorption.</figcaption></figure>
### Phase I (0 to 10 min): Rapid Initial Adsorption

This phase is characterized by a very high biosorption rate, as reflected in the steep rise in the adsorption curve. During the initial 10 min, there are many vacant adsorption sites on the surface of the adsorbent, allowing the adsorbate molecules (either BF or MB) to be rapidly captured. The adsorption process is fast because of the abundance of unoccupied sites available for the adsorbates, and there are minimal interactions between the adsorbed molecules at this stage. The molecules easily diffuse to the available sites on the adsorbent surface, leading to a sharp increase in the amount of adsorbed material. This phase reflects the high availability of free sites, allowing for quick adsorption.

### Phase II (10 to 30 min for both NBio and CBio): Slower Adsorption

In the second phase, the rate of biosorption slows significantly. This is due to the fact that a large portion of the surface sites are already occupied by the adsorbate molecules, leaving fewer sites available for further adsorption. As more molecules adsorb, the repulsive forces between the adsorbed molecules start to become significant. These repulsive interactions between the adsorbate molecules hinder the access of new adsorbate molecules to the available sites. The rate of adsorption continues to decrease as the system moves closer to equilibrium. This phase typically represents the transition from the rapid initial adsorption to the more gradual filling of the remaining adsorption sites.

During this stage, the adsorbent surface is being saturated, and fewer binding sites are available for the remaining molecules. The adsorption process becomes progressively slower due to the increasing resistance to adsorption and the greater tendency for already adsorbed molecules to repel additional molecules. The overall decrease in the rate of biosorption in this phase suggests that the system is approaching saturation [58].

### Final Phase (after 60 min for both NBio and CBio): Equilibrium State

In the final phase, after 60 min, the adsorption process reaches equilibrium. This stage is marked by a stabilization of the adsorption rate, where the number of molecules adsorbed onto the surface equals the number of molecules desorbed. The surface sites of the adsorbent are fully occupied, meaning no further adsorption can occur under the experimental conditions. At this point, the adsorption capacity of the biosorbent is reached. For both NBio and CBio, the adsorption capacities are measured as 9.001 mg g⁻¹ and 8.912 mg g⁻¹, respectively, for BF, and 9.05 mg g⁻¹ and 8.24 mg g⁻¹ for MB. These values represent the maximum amount of adsorbate that can be held by the adsorbent at equilibrium.

It is also worth noting that the equilibrium time of 60 min is consistent with findings from other studies in the literature, where similar adsorption processes have been observed to reach equilibrium within this timeframe. This suggests that 60 min is a suitable duration for the adsorption process to stabilize under the experimental conditions used in this study.

In summary, the adsorption process progresses through three stages. Initially, rapid adsorption occurs as there are abundant free sites for the adsorbate molecules. As more molecules adsorb, the process slows down due to the occupation of surface sites and the repulsive forces between adsorbate molecules. Finally, the process reaches equilibrium when the adsorbent surface is saturated with adsorbate molecules, and no further adsorption takes place. These observations confirm that the biosorption of BF and MB on NBio and CBio follows a well-defined kinetic pattern with clear phases of rapid adsorption, slowing as sites fill, and eventual equilibrium. The adsorption capacities at equilibrium provide valuable information for the potential application of these biosorbents in real-world adsorption processes.
### 3.5.2. Effect of Initial Concentration

In Figure 5, the biosorption capacity for both NBio and CBio demonstrates a clear positive correlation with the initial concentrations of BF and MB. This trend is attributed to the higher availability of biosorption sites compared to the concentration of dye molecules in the solution. As the concentration of the dyes increases, more molecules diffuse from the solution to the adsorbent surface, resulting in an enhanced adsorption rate. The initial phase of biosorption is rapid, as there are plenty of unoccupied sites for the dye molecules to bind. However, as more dye molecules are adsorbed, the adsorption rate starts to decrease as the available surface sites become increasingly occupied.

<figure><img src="image_7.png" /><figcaption>Figure 5. Impact of the BF (a) and MB (b) initial concentrations on biosorption.</figcaption></figure>

This behavior confirms that biosorption is highly dependent on the initial concentration of the dye solution, as is commonly observed in the literature [59]. At higher initial dye concentrations, typically greater than 100 mg L⁻¹, the adsorption process eventually reaches a steady state. This steady state signifies that all the available biosorption sites on the adsorbent have been filled, and no further dye molecules can be adsorbed. Consequently, this leads to the attainment of the saturation point, where the biosorbent can no longer effectively adsorb additional dye molecules, and the process of adsorption slows down. In this study, the saturation concentration was identified as 100 mg L⁻¹, which coincides with similar findings reported in various research articles. Such saturation concentrations represent the point at which the adsorbent reaches its maximum adsorption capacity, after which any increase in the initial dye concentration will not significantly affect the adsorption rate. This saturation behavior is essential in optimizing the biosorption process for practical applications, ensuring that the adsorbent's capacity is fully utilized without excessive waste [60].
### 3.5.3. Effect of the Amount of Biosorbent

The data presented in Figure 6 indicate that as the amount of biosorbent is increased, the biosorption capacity tends to decrease (Figure 6a,b). This observation suggests that an excessive amount of biosorbent may lead to the agglomeration of its particles, which reduces the overall surface area available for dye molecules to interact with. When the particles cluster together, there is a smaller area for the dye molecules to adhere to, and this, in turn, increases competition among the dye molecules trying to access these limited adsorption sites. As a result, the biosorption process becomes less efficient [61]. This phenomenon of particle agglomeration and its negative impact on adsorption capacity has also been reported in other studies. Furthermore, a comparable pattern of reduced adsorption efficiency was observed for MB adsorption on Safi clay in a study by Karim et al. [62] and Mohammad et al. [63], indicating that this issue is not unique to the current biosorbents but might be a general trend observed with various adsorbents.

<figure><img src="image_8.png" /><figcaption>**Figure 6.** Effect of the biosorbent mass on BF (a) and MB (b) biosorption.</figcaption></figure>

In terms of discoloration yield (DY), as shown in Figure 6, the best results were achieved with 0.05 g of biosorbent, which demonstrated approximately 90% of discoloration for both BF and MB dyes. This suggests that 0.05 g is the optimal amount of biosorbent for achieving high biosorption efficiency. Therefore, this value was selected as the optimal biosorbent mass for further experimental work, providing a balance between an adequate surface area for adsorption and the efficient use of the biosorbent material.
### 3.6. Equilibrium Study

The analysis of the biosorption data using the Langmuir isotherm was carried out by plotting 1/Qe against 1/Ce, as shown in Figure 7a,b. The linearity of these plots enables the determination of the Qm and the Langmuir constant, as well as the correlation coefficients. These values, summarized in Table 3, indicate the goodness of fit for the Langmuir model in describing the biosorption equilibrium of the dyes (BF and MB) on both NBio and CBio. The high correlation coefficients (0.97 for BF and 0.98 for MB) demonstrate that the Langmuir model adequately describes the adsorption process, confirming that the biosorption follows a monolayer adsorption mechanism with a uniform distribution of adsorption sites. The RL values, ranging between 0 and 1, further support the conclusion that the biosorption process is favorable. An RL value in this range suggests that the process is reversible and that the adsorption of BF and MB on both biosorbents is efficient and favorable, as evidenced by previous studies in similar contexts [28].

<figure><img src="image_9.png" /><figcaption>**Figure 7.** Isotherm plots for biosorption of dyes on both native ((a) Langmuir and (c) Freundlich) and calcined biomasses ((b) Langmuir and (d) Freundlich).</figcaption></figure>

In addition to the Langmuir model, the Freundlich isotherm was also applied to the data. Figure 7c,d present linear plots of 1/Qe versus 1/Ce, which are used to derive the Freundlich constants, 1/n and Kf. These parameters provide insight into the nature of the adsorption process. The 1/n parameter, in particular, is indicative of the adsorption intensity and the heterogeneity of the biosorption sites. A value of 1/n less than 1 indicates favorable adsorption, which is consistent with the results obtained for both dyes on NBio and CBio. In this study, all 1/n values were found to be less than 1, confirming the favorable adsorption of BF and MB on both biosorbents, in agreement with the RL values derived from the Langmuir model. The favorable adsorption characteristics are further corroborated by the magnitude of Kf, which reflects the adsorption capacity.
<table><caption>**Table 3.** Isotherm models' parameters and correlation coefficients for the biosorption of BF and MB on both native and calcined biomasses.</caption><thead><tr><th rowspan="2">Adsorbent</th><th rowspan="2">Isotherm</th><th rowspan="2">Parameters</th><th colspan="2">Dyes</th></tr><tr><th>BF</th><th>MB</th></tr></thead><tbody><tr><td rowspan="6">NBio</td><td rowspan="4">Langmuir</td><td>Q<sub>m</sub> (mg g<sup>-1</sup>)</td><td>111</td><td>111.11</td></tr><tr><td>K<sub>L</sub> (L mg<sup>-1</sup>)</td><td>0.20</td><td>0.12</td></tr><tr><td>R<sub>L</sub></td><td>0.20</td><td>0.29</td></tr><tr><td>R<sup>2</sup></td><td>0.99</td><td>0.99</td></tr><tr><td rowspan="3">Freundlich</td><td>K<sub>f</sub> (mg g<sup>-1</sup>)</td><td>22.65</td><td>15.62</td></tr><tr><td>1/n</td><td>0.42</td><td>0.53</td></tr><tr><td>R<sup>2</sup></td><td>0.83</td><td>0.94</td></tr><tr><td rowspan="6">CBio</td><td rowspan="4">Langmuir</td><td>Q<sub>m</sub> (mg g<sup>-1</sup>)</td><td>100</td><td>142.85</td></tr><tr><td>K<sub>L</sub> (L mg<sup>-1</sup>)</td><td>0.16</td><td>0.07</td></tr><tr><td>R<sub>L</sub></td><td>0.23</td><td>0.39</td></tr><tr><td>R<sup>2</sup></td><td>0.94</td><td>0.90</td></tr><tr><td rowspan="3">Freundlich</td><td>K<sub>f</sub> (mg g<sup>-1</sup>)</td><td>17.35</td><td>13.80</td></tr><tr><td>1/n</td><td>0.53</td><td>0.60</td></tr><tr><td>R<sup>2</sup></td><td>0.72</td><td>0.78</td></tr></tbody></table>

The coefficient of determination (R²) values obtained for both models provide a quantitative measure of how well the experimental data fit the theoretical isotherms. For both NBio and CBio, the Langmuir model exhibits strong coefficients of determination, indicating a well-defined monolayer adsorption process. However, when comparing the two models, it is evident that the Freundlich model better describes the adsorption on NBio, as indicated by higher R² values in comparison to CBio. This suggests that the adsorption on NBio is more heterogeneous, with a broader range of adsorption sites and varying adsorption energies. In contrast, the biosorption process on CBio is more uniform and follows the Langmuir model more closely, suggesting fewer variations in adsorption sites and energies.

Overall, the combination of the Langmuir and Freundlich models provides valuable insights into the nature of the biosorption processes, indicating that both biosorbents exhibit favorable adsorption properties, with NBio demonstrating more heterogeneity in adsorption sites and CBio showing a more uniform adsorption process.

The Qm values of the NBio and CBio adsorbents, determined from the Langmuir model, are higher than those of some reported adsorbents for MB and BF removal, as shown in Table 4. These higher values are related to the crystallinity and the morphology of the NBio and CBio adsorbents shown in Sections 3.1 and 3.3, respectively, which are different from those of other adsorbents. These findings indicate that NBio and CBio are economic, effective, and eco-friendly new materials to be utilized for the adsorption of dyes, especially MB and BF.

<table><caption>**Table 4.** Comparison of adsorption capacities of NBio and CBio with other adsorbents.</caption><thead><tr><th>Dye</th><th>Adsorbent</th><th>Q<sub>m</sub> (mg g<sup>-1</sup>)</th><th>Reference</th></tr></thead><tbody><tr><td rowspan="6">MB</td><td>Corncob-activated carbon</td><td>82.71</td><td>[64]</td></tr><tr><td><i>Punica granatum</i> L. seeds</td><td>99.01</td><td>[65]</td></tr><tr><td>Walnut shell powder</td><td>36.63</td><td>[63]</td></tr><tr><td>Loofah (<i>Luffa cylindrica</i>)</td><td>1.74</td><td>[29]</td></tr><tr><td>NBio</td><td>111.11</td><td>This study</td></tr><tr><td>CBio</td><td>142.85</td><td>This study</td></tr></tbody></table>
<table><caption>**Table 4.** *Cont.*</caption><thead><tr><th>Dye</th><th>Adsorbent</th><th>Q<sub>m</sub> (mg g<sup>-1</sup>)</th><th>Reference</th></tr></thead><tbody><tr><td rowspan="5">BF</td><td>Soybean straw hydrolyzed</td><td>72.9</td><td>[66]</td></tr><tr><td>Mussel-powdered eggshell membrane</td><td>48</td><td>[46]</td></tr><tr><td>Loofah (Luffa cylindrica)</td><td>1.64</td><td>[29]</td></tr><tr><td>NBio</td><td>111</td><td>This study</td></tr><tr><td>CBio</td><td>100</td><td>This study</td></tr></tbody></table>

### 3.7. Kinetic Study

The kinetic analysis of biosorption provides crucial insights into the mechanisms and dynamics governing the adsorption process. In this study, two widely used kinetic models, the pseudo-first-order and pseudo-second-order models, were applied to evaluate the adsorption behaviors of BF and MB onto NBio and CBio.

#### 3.7.1. Analysis of the Pseudo-First-Order Model

The linear form of the pseudo-first-order model, illustrated in Figure 8a,d, highlights the limitations of this approach in describing the experimental data. The R² for this model ranged from 0.69 to 0.87, suggesting a moderate fit at best. More critically, the calculated adsorption capacities ($Q_e$ (th)) derived from this model deviate significantly from the experimentally measured values ($Q_e$ (ex)). This discrepancy indicates that the pseudo-first-order model does not accurately represent the adsorption mechanism for either BF or MB on the biosorbents studied.

<figure><img src="image_10.png" /><figcaption>**Figure 8.** Kinetic model plots for the biosorption of MB and BF on both native (a) first order, (b) second order, and (c) intra-particle diffusion) and calcined biomasses (d) first order, (e) second order, and (f) intra-particle diffusion).</figcaption></figure>
Such a mismatch between the calculated and experimental values points to the inadequacy of the pseudo-first-order model in capturing the underlying kinetics of the adsorption process. This conclusion aligns with previous studies reporting similar findings. For instance, the adsorption of safranin-O onto pineapple peels was found to be poorly described by the pseudo-first-order model [67], as was the adsorption of MB onto microwave-irradiated hydroxyapatite [68]. These results collectively suggest that the pseudo-first-order model is not suitable for adsorption processes involving complex biosorbents like NBio and CBio.

### 3.7.2. Analysis of the Pseudo-Second-Order Model

In contrast, the pseudo-second-order model provided a much better representation of the experimental data, as shown in Figure 8b,e. The rate constants and adsorption capacities calculated using this model are presented in Table 5. Notably, the calculated adsorption capacities ($Q_e$ (th)) for BF and MB closely match the experimental values ($Q_e$ (ex)). This agreement underscores the validity of the pseudo-second-order model in describing the adsorption kinetics.

<table><caption>**Table 5.** Kinetic models' parameters and correlation coefficients for the biosorption of dyes on native and calcined biomasses ($C_0$ = 10 mg L⁻¹; T = 25 °C; initial pH (MB = 6.60, BF = 8.53)).</caption><thead><tr><th rowspan="2">Order of the Reaction</th><th rowspan="2">Parameter</th><th colspan="2">NBio</th><th colspan="2">CBio</th></tr><tr><th>BF</th><th>MB</th><th>BF</th><th>MB</th></tr></thead><tbody><tr><td rowspan="4">Pseudo-first order</td><td>K<sub>1</sub> (min<sup>-1</sup>)</td><td>0.04</td><td>0.02</td><td>0.04</td><td>0.01</td></tr><tr><td>Q<sub>e</sub> (ex) (mg g<sup>-1</sup>)</td><td>9.00</td><td>9.05</td><td>8.88</td><td>8.24</td></tr><tr><td>Q<sub>e</sub> (the) (mg g<sup>-1</sup>)</td><td>1.67</td><td>1.37</td><td>1.21</td><td>1.37</td></tr><tr><td>R<sup>2</sup></td><td>0.87</td><td>0.84</td><td>0.71</td><td>0.69</td></tr><tr><td rowspan="4">Pseudo-second order</td><td>K<sub>2</sub> (min<sup>-1</sup>)</td><td>0.11</td><td>0.38</td><td>0.30</td><td>0.73</td></tr><tr><td>Q<sub>e</sub> (exp) (mg g<sup>-1</sup>)</td><td>9.00</td><td>9.05</td><td>8.88</td><td>8.24</td></tr><tr><td>Q<sub>e</sub> (the) (mg g<sup>-1</sup>)</td><td>9.09</td><td>9.05</td><td>8.93</td><td>8.22</td></tr><tr><td>R<sup>2</sup></td><td>0.99</td><td>1</td><td>0.99</td><td>0.99</td></tr><tr><td rowspan="3">Intra-particle diffusion</td><td>K (mg g<sup>-1</sup> min<sup>-1/2</sup>)</td><td>0.69</td><td>0.74</td><td>0.63</td><td>0.64</td></tr><tr><td>C</td><td>4.51</td><td>4.70</td><td>4.32</td><td>4.45</td></tr><tr><td>R<sup>2</sup></td><td>0.50</td><td>0.43</td><td>0.42</td><td>0.39</td></tr></tbody></table>

Moreover, the value of R² for the pseudo-second-order model exceeded 0.8 for all cases, indicating a strong linear relationship and a superior fit compared to the pseudo-first-order model. This high degree of correlation demonstrates the model's ability to accurately predict the dynamics of the adsorption process. The pseudo-second-order model's reliability is further supported by its frequent application in similar studies. For example, the adsorption of MB onto low-cost adsorbents has been shown to conform well to the pseudo-second-order model [69]. Additionally, earlier research has highlighted the model's effectiveness in describing adsorption processes involving solutes in solution [70].

### 3.7.3. Mechanistic Implications

The superior fit of the pseudo-second-order model suggests that the adsorption process is likely governed by chemisorption, involving the sharing or exchange of electrons between the dye molecules and the active sites on the biosorbent surfaces. The possible interactions between MB and hydroxyapatite (that is, the principal constituent of bone) are shown in Figure 9. This mechanism is consistent with the model's assumption that adsorption is controlled by the availability of active sites and the interaction energy between adsorbent and adsorbate.
<figure><img src="image_11.png" /><figcaption>**Figure 9.** Mechanism of methylene blue sorption on hydroxyapatite.</figcaption></figure>

The findings also indicate that the adsorption process is not solely influenced by the physical characteristics of the biosorbents but also by the chemical interactions occurring at the surface. For NBio and CBio, the differences in surface morphology, as previously characterized, could further influence the adsorption dynamics and contribute to the observed kinetics.

The kinetic analysis confirms that the pseudo-second-order model provides a more accurate and reliable description of the adsorption process for BF and MB onto NBio and CBio than the pseudo-first-order model. These results not only validate the applicability of the pseudo-second-order model but also offer insights into the adsorption mechanism, suggesting chemisorption as the dominant process. Such findings are invaluable for optimizing biosorption systems and developing more effective biosorbents for dye removal in wastewater treatment applications.

The parameters of the intra-particle diffusion model, namely the intercept (C) and the diffusion rate constant ($K_{id}$), were determined from the linear segments of the plots in Figure 8c,f. These plots represent the relationship between the amount of dye adsorbed over time and the square root of time, following the intra-particle diffusion model. The corresponding values are compiled in Table 5 for both NBio and CBio biosorbents.

The C parameter reflects the contribution of the boundary layer to the overall biosorption process. A higher C value implies a stronger boundary layer effect, which limits the penetration of dye molecules into the inner pores of the biosorbent [71]. In this study, the intercept values for all samples exceed 4, indicating a significant boundary layer influence. Additionally, the low correlation coefficients, all below 0.5, further confirm that the intra-particle diffusion is not the sole mechanism governing the biosorption process.

This observation suggests that the biosorption of BF and MB on both NBio and CBio involves multiple mechanisms, with the boundary layer playing a predominant role in
restricting dye molecule diffusion into the pores. Consequently, the adsorption process cannot be accurately described solely by the intra-particle diffusion model.

Comparable trends have been documented in the literature. For example, Benaissa et al. [21] reported a similar boundary layer effect in the biosorption of MB and BF onto Luffa cylindrica. Jia et al. [56] observed analogous results for MB adsorption onto bone char, where the intra-particle diffusion model was insufficient to fully describe the process due to significant boundary layer influences.

These findings underline the complex nature of the biosorption process, where factors such as surface characteristics, pore accessibility, and molecular interactions with the boundary layer collectively determine the adsorption efficiency. This highlights the importance of employing complementary models and analyses to gain a comprehensive understanding of the underlying mechanisms in biosorption systems.

### 3.8. *Thermodynamic Study*

The thermodynamic analysis provides crucial insights into the nature of the biosorption processes for MB and BF on both NBio and CBio. These parameters, derived from the linear plots of ln K<sub>d</sub> versus 1/T (Figure 10), include enthalpy (enthalpy (ΔH°), entropy (ΔS°), and free energy (ΔG°)), and their calculated values are presented in Table 6.

<figure><img src="image_12.png" /><figcaption>**Figure 10.** Plot of Ln (K<sub>d</sub>) as a function of (1/T) for FB (a) and MB (b).</figcaption></figure>
<table><caption>**Table 6.** Thermodynamic parameters of FB and MB sorption by native and calcined biomasses.</caption><thead><tr><th rowspan="2">Adsorbent</th><th colspan="2">ΔH° (kJ mol<sup>-1</sup>)</th><th colspan="2">ΔS° (J mol<sup>-1</sup> K<sup>-1</sup>)</th><th colspan="3">ΔG° (kJ mol<sup>-1</sup>)</th></tr><tr><th>BF</th><th>MB</th><th>BF</th><th>MB</th><th>T (K)</th><th>BF</th><th>MB</th></tr></thead><tbody><tr><td rowspan="4">NBio</td><td rowspan="4">-31.52</td><td rowspan="4">-21.65</td><td rowspan="4">-88.6</td><td rowspan="4">-57.44</td><td>283</td><td>-5.90</td><td>-5.02</td></tr><tr><td>298</td><td>-6.09</td><td>-5.24</td></tr><tr><td>318</td><td>-7.29</td><td>-3.19</td></tr><tr><td>328</td><td>-2.29</td><td>-2.73</td></tr><tr><td rowspan="4">CBio</td><td rowspan="4">16.34</td><td rowspan="4">-18.38</td><td rowspan="4">73.62</td><td rowspan="4">-47.72</td><td>283</td><td>-4.31</td><td>-4.78</td></tr><tr><td>298</td><td>-5.81</td><td>-4.50</td></tr><tr><td>318</td><td>-7.29</td><td>-3.19</td></tr><tr><td>328</td><td>-7.52</td><td>-2.75</td></tr></tbody></table>

### 3.8.1. Biosorption on NBio

For NBio, the negative ΔH° values indicate that the biosorption is both physical in nature and exothermic. This suggests that the interaction forces between the adsorbent (NBio) and the dye molecules are dominated by van der Waals forces, hydrogen bonding, or electrostatic interactions, which do not require significant energy input. The process releases heat, further confirming its exothermic nature.

The negative ΔS° values imply an increase in the order at the interface between the adsorbent and the adsorbate. This could be attributed to the structuring or alignment of the dye molecules on the biosorbent surface. Such structuring often occurs due to strong binding or the orientation of the adsorbate molecules, potentially involving rearrangement at the molecular level or even weak chemical bond formations, as highlighted by Yang et al. [72].

The spontaneity of the biosorption is supported by the negative ΔG° values, which indicate that the process is thermodynamically favorable under the studied conditions. The combined effect of exothermic heat release and increased interfacial order suggests a robust interaction mechanism for NBio.

### 3.8.2. Biosorption on CBio

In contrast, the biosorption process on CBio exhibits distinctly different thermodynamic characteristics. The positive ΔH° values signify an endothermic process, implying that the adsorption requires external energy input. This is typical of processes where adsorbate molecules overcome repulsive forces or desolvation barriers before adhering to the adsorbent surface. The endothermic nature may also suggest weaker initial interactions compared to NBio, requiring energy to facilitate adsorbent-adsorbate contact.

The positive ΔS° values reflect an increase in randomness or disorder at the solid-liquid interface. According to Amellal et al. [73], this increase could stem from the displacement of water molecules or the desolvation of dye molecules as they migrate from the bulk solution to the biosorbent surface. Additionally, surface structural changes in CBio or the partial aggregation of dye molecules on the adsorbent could contribute to the observed entropy gain.

Despite the endothermic nature of the process, the negative ΔG° values confirm the feasibility and spontaneity of the biosorption under the experimental conditions. This indicates that the entropy gain, rather than the enthalpy change, drives the biosorption process for CBio.

### 3.8.3. Comparative Analysis

The contrasting thermodynamic behaviors of NBio and CBio underline their distinct adsorption mechanisms. For NBio, the exothermic and ordered process points to strong
and favorable interactions between the adsorbent and the dye molecules, emphasizing its efficiency in adsorption. Conversely, the endothermic and entropy-driven process on CBio suggests a greater reliance on external energy and surface modifications to facilitate adsorption. This distinction highlights the importance of selecting suitable biosorbents based on the desired thermodynamic profile for specific applications.

In conclusion, the thermodynamic parameters not only validate the feasibility and spontaneity of the biosorption processes for both NBio and CBio but also provide a deeper understanding of the underlying mechanisms. These findings can guide the optimization of biosorption systems for dyes and other pollutants in wastewater treatment.

### 3.9. Decision Tree Modeling

The optimization results presented in Table 7 for the best DT_LSBOOST model provide valuable insights into the model's performance and predictive capabilities. The Min. Leaf Size parameter is set to 1, meaning that the Decision Tree can create leaf nodes with very small data subsets. This setting allows the tree to capture detailed patterns in the data, which can be beneficial for making highly specific predictions. However, it also increases the potential for overfitting if the model becomes too tailored to the training data. In this case, the low RMSE and high R values on the validation data suggest that the model has avoided overfitting, implying it has generalization capabilities despite the sensitivity to small data subsets.

<table><caption>**Table 7.** Performances of the best model of DT_LSBOOST.</caption><thead><tr><th rowspan="2">Min. Leaf Size</th><th rowspan="2">Learning Rate</th><th rowspan="2">Surrogate</th><th rowspan="2">Min. Parent Size</th><th rowspan="2">Number of Learning Cycles</th><th rowspan="2">Max. Number Splits</th><th rowspan="2">Number of Nodes</th><th colspan="3">Coefficients of Correlation</th><th colspan="3">RMSE</th></tr><tr><th>APP</th><th>VAL</th><th>ALL</th><th>APP</th><th>VAL</th><th>ALL</th></tr></thead><tbody><tr><td>1</td><td>0.1</td><td>ALL</td><td>2</td><td>10</td><td>120</td><td>97</td><td>0.9999</td><td>0.9999</td><td>0.9999</td><td>0.0031</td><td>0.0029</td><td>0.0030</td></tr></tbody></table>

The learning rate of 0.1 in the LSBoost algorithm plays a crucial role in controlling the magnitude of updates made during each boosting iteration. This learning rate value indicates a balance between making significant improvements to the model without overshooting or converging too slowly. A moderate learning rate like this ensures that the model iteratively corrects its errors while maintaining stability, resulting in a refined predictive model. This helps avoid instability, allowing for a steady improvement in the model's performance over multiple boosting cycles.

The Surrogate = "ALL" setting allows the model to use Surrogate splits when the primary split is not available due to missing data. This increases the model's robustness by ensuring that the Decision Tree can still function effectively even when some data points are missing. The ability to use Surrogate splits also reduces the likelihood of prediction failure when the data are incomplete, ensuring that the model remains stable and continues to make predictions in the presence of such challenges. This feature contributes to the overall reliability and adaptability of the model.

The Min. Parent Size parameter is set to 2, meaning that a node will only split if there are at least two samples in the parent node. This restriction helps prevent overfitting by ensuring that splits are only made when there is sufficient data to support them. A lower Min. Parent Size allows for a more detailed model, but with this setting, the model avoids creating overly specific splits based on too few data points, striking a balance between model complexity and generalization.

The Number of Learning Cycles is set to 10, indicating that the model undergoes 10 iterations in the boosting process. Each cycle corrects the errors made by the previous cycle, which allows the model to progressively refine its predictions. A higher number of cycles allows the model to learn from residual errors, improving the accuracy and reducing
bias. The relatively high number of cycles indicates that the model has undergone extensive learning, which has likely contributed to its superior performance.

The max. number of splits is set to 97, which allows the tree to make a significant number of splits. A higher number of splits gives the model the flexibility to capture complex relationships between the input variables. While a large number of splits can lead to overfitting, the performance metrics on the validation data suggest that the model has been able to capture complex patterns while maintaining generalization. This suggests that the model structure is appropriate for the complexity of the data.

The exact number of nodes is not provided in Table 7, but it can be inferred that the tree has a relatively high number of nodes based on the maximum number of splits. Each node represents a decision point in the tree, and the number of nodes typically increases with the number of splits. A higher number of nodes reflects a more detailed tree structure capable of capturing intricate relationships in the data.

The R values for the application, validation, and all datasets are exceptionally high, with values of 0.9999. This indicates that the model has a near-perfect fit to the data, meaning it explains nearly all of the variance in the target variable. The high R values across the different subsets (training, validation, and testing) highlight the robustness of the model, suggesting that it is highly reliable in both training and real-world applications.

The RMSE values for the training, validation, and testing datasets are all very low, with values of 0.0031, 0.0029, and 0.0030, respectively. RMSE is a common metric for assessing the accuracy of a model's predictions, and these low values indicate that the model's predictions are very close to the actual values. The small RMSE values across all datasets demonstrate that the model is highly accurate and that its predictions are consistent and reliable, further confirming the model's ability to generalize well to new, unseen data.

The optimization results of the DT LSBOOST model demonstrate that it is an exceptionally effective predictive tool, providing highly accurate predictions with minimal errors. The fine-tuning of the hyperparameters such as the learning rate, the Number of Learning Cycles, and the max. number of splits has resulted in a model that balances complexity and generalization. The high coefficients of correlation and the low RMSE values indicate that the model has learned the underlying patterns in the data and can make precise predictions. This performance reflects the model's suitability for accurately predicting the adsorption capacities for the removal of methylene blue and basic fuchsin dyes, showcasing its potential for real-world applications.

Figure 11 represents the results of the decision tree model graphically (the predicted values vs. the experimental values).

<figure><img src="image_13.png" /><figcaption>Figure 11. *Cont.*</figcaption></figure>
<figure><img src="image_14.png" /><figcaption>**Figure 11.** Relationship between the experimental and the DT LSBOOST model predicted values: (a) training data, (b) validation data, and (c) all data.</figcaption></figure>

### 3.9.1. Performance of DT LSBOOST Model on Unseen Testing Data

To assess the effectiveness of the obtained model, the 15% of the dataset that was previously withheld was used for testing. This approach ensures that the model is evaluated on data it has not seen during training, providing a more accurate measure of its predictive capabilities in real-world conditions. By using this unseen portion of the data, the model's ability to generalize to new, unseen instances is tested, which is crucial for determining its practical applicability.

The results obtained from testing the model on the unseen testing data are summarized in Table 8. Table 8 presents key performance metrics such as R and RMSE that reflect the model's accuracy and robustness in predicting the adsorption capacity for the removal of MB and BF dyes. These metrics allow for a direct comparison of the model's performance on the test data against its performance on the training and validation sets.

<table><caption>**Table 8.** DT LSBOOST model performance on unseen testing data.</caption><thead><tr><td>R</td><td>RMSE</td></tr></thead><tbody><tr><td>0.9999</td><td>0.0029</td></tr></tbody></table>

The testing phase provides valuable insights into the model's real-world performance. If the performance metrics on the testing dataset are consistent with those obtained during training and validation, they indicate that the model is not overfitting and is capable of making reliable predictions on unseen data. Conversely, large discrepancies between the
test results and the training results may suggest that the model is overfitting and that further adjustments to the model's parameters or data preprocessing may be necessary.

In the case of this study, the performance of the model on the unseen testing dataset, as shown in Table 8, should demonstrate the model's predictive accuracy and its ability to maintain low error rates across different datasets. The goal is to confirm that the model can consistently predict the adsorption quantities for both native and calcined chicken bioadsorbents, as well as for both MB and BF dyes, under varying experimental conditions. This validation of the model's predictive power on unseen data strengthens its potential for practical applications in environmental or industrial settings where similar data characteristics may arise.

By testing the model in this way, this study ensures that the predictive model is not only accurate within the bounds of the training data but also robust enough to handle new, potentially more complex scenarios. This process of testing with previously unseen data is critical for determining the true effectiveness of any predictive model.

The results presented in Table 8 show the DT LSBOOST model's performance on the unseen test data. The two key metrics, R and RMSE, provide important insights into the model's predictive accuracy on the unseen testing dataset.

The R value of 0.9999 indicates an almost perfect fit between the model's predictions and the actual test data. This coefficient of determination suggests that the model is able to explain 99.99% of the variance in the test dataset. Such a high value is indicative of a highly accurate model that can generalize well to new, unseen data. The close match between the predicted and actual values reflects the model's exceptional predictive power, ensuring that it maintains consistency and reliability even when applied to previously unseen instances.

The RMSE value of 0.0029 is also very low, which is an indication of the model's high accuracy. The RMSE measures the average magnitude of the errors between predicted and actual values, with lower values representing better model performance. In this case, an RMSE of 0.0029 indicates that the model's predictions deviate only slightly from the actual values, suggesting minimal error and a high level of precision in the predictions. This further reinforces the model's reliability and accuracy in predicting adsorption quantities for both native and calcined chicken bioadsorbents for the removal of methylene blue and basic fuchsin dyes.

The results from Table 8 demonstrate that the DT LSBOOST model has achieved exceptional performance in predicting the adsorption quantities in the test dataset. The near-perfect R value and the low RMSE confirm that the model is both highly accurate and capable of generalizing well to new data, indicating that it is well suited for practical applications in similar predictive tasks.

To provide a visual representation of these performances, experimental values and predicted values have been graphically represented in Figure 12.

<figure><img src="image_15.png" /><figcaption>**Figure 12.** Comparison between experimental and predicted values to assess the performance of the DT LSBOOST.</figcaption></figure>
### 3.9.2. Residues Study

In this section, a thorough and comprehensive evaluation was performed to rigorously assess the performance and effectiveness of the chosen model. This process included the application of both the residual method and an error histogram, covering crucial stages such as training, validation, and testing. A detailed comparative analysis was then carried out by comparing experimental values with predicted ones, encompassing all data points from the training, validation, and testing datasets, as shown in Figure 13a. Furthermore, a precise error quantification was performed by examining the discrepancies between experimental and predicted values across the entire dataset, including the training, validation, and testing sets, following established methodologies. The results of this in-depth error evaluation are clearly visualized in Figure 13b, using advanced residual analysis techniques.

<figure><img src="image_16.png" /><figcaption>**Figure 13.** Residuals relating to the models established by the different techniques according to the estimated values: (a) relationship between experimental data and the predicted data of samples, and (b) instances of distribution of errors.</figcaption></figure>
The results of the two figures provide valuable insights into the performance of the model. In Figure 13a, the experimental values are superimposed with the predicted ones, and we observe a strong alignment between the two datasets. This close overlap suggests that the model's predictions are highly accurate, with minimal deviation from the actual experimental values. The near-perfect alignment indicates that the model has successfully captured the underlying patterns in the data and is capable of making reliable predictions for unseen data points.

Figure 13b displays the error analysis with the discrepancies circled around zero. It can be interpreted that the majority of the errors are very small and centered around zero. This suggests that the model's predictions are consistently close to the actual values, with only minor errors. The fact that the errors are centered around zero implies that the model does not show any significant bias, either overestimating or underestimating the predictions, which is a desirable characteristic for predictive models.

Together, these two figures demonstrate that the model is highly effective and accurate, as evidenced by the minimal errors and the close fit between the predicted and experimental values. The results indicate that the model has a strong generalization capability, making it well suited for predictive tasks in similar scenarios.

### 3.9.3. Interface for Optimization and Prediction

A MATLAB-based application has been developed to predict the adsorption quantity of CBio and NBio for the removal of MB and BF dyes, leveraging the DT_LSBOOST model (Figure 14). The application is designed to be straightforward and user-friendly, requiring only the input of several key parameters for an accurate prediction. Specifically, users are prompted to enter the contact time, adsorbent mass, and dye concentration, which are the primary factors influencing the adsorption process. Additionally, the user must specify the type of adsorbent used, whether CBio or NBio, and the dye type, either MB or BF. With these input values, the application automatically processes the data through the trained DT_LSBOOST model, producing the predicted adsorption quantity for the specified conditions. This tool simplifies the prediction process, offering an accessible means for researchers and practitioners to estimate adsorption efficiency without needing to manually run complex calculations or experiments. The model's high accuracy, as demonstrated through prior evaluations, ensures reliable predictions, making the application a valuable resource for optimizing the adsorption-based removal of dyes from aqueous solutions.

<figure><img src="image_17.png" /><figcaption>**Figure 14.** MATLAB interface for predicting MB and BF adsorption by native and calcined biomasses using DT_LSBOOST.</figcaption></figure>
## 4. Conclusions

This study highlights the potential of chicken bone biomass, processed in native (NBio) and calcined (CBio) forms, as an innovative and sustainable solution for wastewater treatment. Through a combination of experimental characterization and advanced modeling, significant findings were established regarding the structural, kinetic, and thermodynamic properties of these biosorbents. Key characterizations demonstrated that calcination profoundly alters the physicochemical properties of the biomass, enhancing its crystallinity and porosity while removing organic impurities. The specific surface area increased substantially from 247 m² g⁻¹ for NBio to 370 m² g⁻¹ for CBio, aligning with the improved adsorption capacities observed for CBio. These structural transformations rendered CBio particularly effective in dye removal, achieving maximum adsorption capacities of 111 mg g⁻¹ for basic fuchsine (BF) and 142.85 mg g⁻¹ for methylene blue (MB). Adsorption kinetics were best described by the pseudo-second-order model, indicating chemisorption as the dominant mechanism. The possible interactions between dyes and the biosorbent are hydrogen bonding, electrostatic interactions, and Lewis acid-base interactions. Equilibrium studies revealed a monolayer adsorption mechanism for CBio (Langmuir isotherm) and heterogeneous adsorption behavior for NBio (Freundlich isotherm). Thermodynamic analysis highlighted fundamental differences between the two biosorbents: while NBio exhibited exothermic and ordered adsorption, CBio demonstrated an endothermic, entropy-driven process. Despite these differences, both materials showed spontaneous adsorption behavior, reinforcing their feasibility for practical applications. The integration of experimental data with a decision tree model coupled with Least Squares Boosting (DT_LSBOOST) provided a powerful predictive framework. The model achieved exceptional accuracy (R² = 0.9999, RMSE < 0.003), reliably forecasting adsorption capacities across varied conditions of dye concentration, contact time, and biosorbent dosage. This tool not only enhances the understanding of adsorption dynamics but also simplifies the practical optimization of dye removal processes. The findings of this study establish chicken bone biomass as a versatile and efficient biosorbent, offering a cost-effective and eco-friendly approach to addressing the growing challenges of water pollution and waste management. By transforming waste materials into high-performance adsorbents, this research aligns with global sustainability goals, promoting circular economy principles and resource recovery. Future studies could further explore the applicability of these biosorbents in removing a broader range of contaminants and assess their performance in real industrial effluents. Additionally, the coupling of biosorption with other treatment technologies, such as advanced oxidation or membrane filtration, presents exciting opportunities for enhanced water purification strategies.

**Author Contributions:** Conceptualization, A.O., Y.Z., H.M., M.K., A.A.A. and Y.B.; writing—original draft preparation, A.O., Y.Z., H.M., M.K. and H.T.; writing—review and editing, A.A.A., Y.B., W.E., L.K., J.Z. and A.A.; supervision, Y.Z., H.M., M.K., A.A.A., Y.B., J.Z., A.A. and H.T.; project administration, Y.Z., H.M., M.K., A.A.A., Y.B., J.Z., A.A. and H.T.; funding acquisition, A.A.A. All authors have read and agreed to the published version of the manuscript.

**Funding:** This work was supported and funded by the Deanship of Scientific Research at Imam Mohammad Ibn Saud Islamic University (IMSIU) (grant number IMSIU-DDRSP2502).

**Data Availability Statement:** The original contributions presented in this study are included in the article. Further inquiries can be directed to the corresponding author.

**Conflicts of Interest:** The authors declare no conflicts of interest.
Nomenclature

<table><tr><td>A</td><td>specific surface area</td></tr><tr><td>AMB</td><td>surface occupied by a molecule of MB</td></tr><tr><td>b</td><td>maximum adsorption capacity</td></tr><tr><td>BF</td><td>basic fuchsine</td></tr><tr><td>CBio</td><td>calcined biomass</td></tr><tr><td>C<sub>i</sub></td><td>initial dye concentration (mg L<sup>-1</sup>)</td></tr><tr><td>C<sub>e</sub></td><td>dye concentration at equilibrium (mg L<sup>-1</sup>)</td></tr><tr><td>C<sub>0</sub></td><td>initial concentration of MB (mg L<sup>-1</sup>)</td></tr><tr><td>d</td><td>the distance between adjacent plane</td></tr><tr><td>DT_LSBOOST</td><td>decision tree with least squares boosting</td></tr><tr><td>FTIR</td><td>Fourier-transform infrared spectroscopy</td></tr><tr><td>hkl</td><td>Miller indices planes</td></tr><tr><td>k<sub>1</sub></td><td>constant of PFO equation (L min<sup>-1</sup>)</td></tr><tr><td>k<sub>2</sub></td><td>constant of PSO equation (L min<sup>-1</sup>)</td></tr><tr><td>K<sub>f</sub></td><td>Freundlich constant (g L mg)</td></tr><tr><td>K<sub>id</sub></td><td>constant of intra-particle diffusion (mg·g<sup>-1</sup>·min<sup>-0.5</sup>)</td></tr><tr><td>KL</td><td>Langmuir constant (L mg<sup>-1</sup>)</td></tr><tr><td>K<sub>d</sub></td><td>distribution coefficient</td></tr><tr><td>LSBoost</td><td>Least Squares Boosting</td></tr><tr><td>MB</td><td>methylene blue</td></tr><tr><td>M</td><td>molar mass of MB</td></tr><tr><td>m</td><td>amount of the biosorbent(g)</td></tr><tr><td>NBio</td><td>native biomass</td></tr><tr><td>N</td><td>Avogadro number</td></tr><tr><td>n</td><td>Freundlich constant</td></tr><tr><td>PFO</td><td>pseudo-first order</td></tr><tr><td>PSO</td><td>pseudo-second order</td></tr><tr><td>Q<sub>e</sub></td><td>amount of dye adsorbed at equilibrium (mg g<sup>-1</sup>)</td></tr><tr><td>Q<sub>t</sub></td><td>quantity adsorbed at time t (mg g<sup>-1</sup>)</td></tr><tr><td>R<sup>2</sup></td><td>correlation coefficient</td></tr><tr><td>RL</td><td>dimensionless separation factor</td></tr><tr><td>R</td><td>perfect gas constant (J mol<sup>-1</sup> k<sup>-1</sup>)</td></tr><tr><td>R</td><td>correlation coefficient of predictive data</td></tr><tr><td>RMSE</td><td>root mean square error of predictions</td></tr><tr><td>SEM</td><td>scanning electron microscopy</td></tr><tr><td>T</td><td>temperature (°C or °K)</td></tr><tr><td>V</td><td>volume of the solution (L)</td></tr><tr><td>XRD</td><td>X-ray diffraction</td></tr><tr><td>β</td><td>full width half maximum</td></tr><tr><td>ΔH°</td><td>enthalpy libre (kJ mol<sup>-1</sup>)</td></tr><tr><td>ΔS°</td><td>entropy (J mol<sup>-1</sup> K<sup>-1</sup>)</td></tr><tr><td>ΔG°</td><td>free energy (kJ mol<sup>-1</sup>)</td></tr></table>

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