Dye Removal from Colored Textile Wastewater Using Seeds and Biochar of Barley (Hordeum vulgare L.)

Abstract

Phenol red (X-PR) and malachite green carbinol (MGC) are two textile finishing dyes, which are present in aquatic environments through industrial effluents. Due to the toxic nature of both dyes, they are harmful to human health. In the present study, two materials, barley seeds and the biochar of barley (Hordeum vulgare L.), were used to remove the dyes in an aqueous solution. The materials used are characterized by AFM, FTIR, SEM, XRD and EDX techniques. In this study, the parameters studied are the adsorbent dose, pH, initial adsorbate concentration and contact time. The maximum equilibrium time was found to be 90 min for all dyes. Kinetic studies revealed that the adsorption of X-PR and MGC on barley seeds (BS-HVL) and the biochar of barley (BC-HVL) followed pseudo-second-order kinetics and that both porous and intraparticle diffusion mechanisms were involved. The adsorption equilibrium data were well fitted to the Langmuir and Freundlich isotherm model for both materials, and the maximum adsorption capacity of monolayer and multilayers for X-PR and MGC were 71.642 mg g⁻¹ and 50 mg g⁻¹ on BS-HVL, and 44.843 mg g⁻¹ and 121.95 mg g⁻¹ on BC-HVL, respectively. The thermodynamic results reveal that the dye removal on barley was endothermic and spontaneous in nature.

1. Introduction

Morocco is one of the countries that places importance on agriculture and the planting of different varieties of barley and wheat. Barley (Hordeum vulgare L.) is the second most cultivated cereal in Morocco after soft wheat. It occupies an average of 1.9 million hectares per year, or 38% of the utilized agricultural area of cereals and 21.8% of the country’s total area. In total 67% of these areas are located in arid and semiarid zones, 8% in mountainous areas, and 24% in areas with low-input soils.

Antioxidant compounds are currently the subject of numerous studies because in addition to their interest in treating a multitude of pathologies, they are also used in the preservation of edible foods for the food industry [1]. The extraction of antioxidants and polyphenols from barley seeds by industry generates nonexploitable wastes; therefore, barley seed extract and its biochar have rarely been proposed for adsorption applications. The aim of this work is to valorize these two materials in order to eliminate two dyes: malachite green and x-phenol red.

Natural substances called bioadsorbents (bioproducts) are applicable for water treatment due to the many advantages and interesting properties of these resources. They are abundant, renewable, biodegradable and inexpensive. From a chemical point of view, they contain macromolecular chains with numerous highly reactive chemical functions. Currently, there is an interest in preparing materials based on polysaccharides, and bioadsorption on these bioadsorbents appears to be a promising method [2,3]. During the last two decades, bioadsorption has proven to be an efficient waste treatment technology [4,5]. Scientists have successfully removed heavy metals and dyes from wastewater using biosorption [6,7]. Recently, there is interest in producing materials based on natural substances such as agricultural waste; in this sense, the bioadsorbents appear to be a very promising method for the adsorption of several dyes [8,9,10,11,12,13]. Similar research shows that activated carbon derived from the barley (Hordeum vulgare L.) husk can be used as an efficient and cost-effective adsorbent for the treatment of phenol-red-contaminated water. Due to their mutagenic and carcinogenic effects, effluents from the dye, paper and textile industries, contaminated with nondegradable organic dyes, not only pose a serious risk to human health but also adversely affect aquatic life. X-phenol red, a finishing textile dye and a pH indicator, is also used in most tissue culture media. The pH-dependent cytotoxicity of contaminants of phenol red for breast cancer cells has previously been reported by Grady et al. [14]. Malachite green is persistently present in the environment and acutely toxic to a wide range of aquatic and terrestrial animals. Several studies have shown that this dye is highly toxic to freshwater fish, both in acute and chronic exposure. Carcinogenesis, mutagenesis, chromosomal fractures, teratogenicity and reduced fertility have also been reported in rainbow trout following treatment with malachite green [15,16,17,18,19,20]. Biomaterials such as barley, due to its microporous structure, high specific surface area and reactivity, play an important role in the adsorption process to remove toxic organic and inorganic chemicals from contaminated water [13].

The aim of this research is to report the synthesis and characterization of barley (Hordeum vulgare L.) seeds and their biochar. The as-synthesized materials have been used as adsorbents for the removal of x-phenol red and malachite green carbinol dyes in an aqueous solution. The effects of various experimental parameters on adsorption of the dyes have been investigated.

2. Materials and Methods

2.1. Materials

The barley used in this study was collected from the northern region of Morocco. It is a biomaterial that is rich in carbon and oxygen as well as minerals. These materials are starch-enriched and deproteinized barley seeds, which we note hereafter by BS-HVL and BC-HVL. The biochar is a carbon-rich product (BC-HVL) which is heated at 600 °C in a closed container with little or no available air. The dyes used in this study are x-phenol red (C₁₉H₁₄O₅S) (MW 354.37 g mol⁻¹, Sigma-Aldrich, St-Louis, MO, USA) and malachite green carbinol (C₂₃H₂₅ClN₂) (MW 364.9 g mol⁻¹, Sigma-Aldrich, St-Louis, MO, USA). The concentration of unabsorbed dyes was determined at 435 nm and 635 nm, respectively, using a UV/visible spectrophotometer. The chemical structures of x-phenol red and malachite green carbinol dyes are given in Figure 1.

2.2. Characterization of BS-HVL and BC-HVL

The seeds and biochar of barley (Hordeum vulgare L.) were characterized by different analytical techniques: X-ray diffraction analysis (Bruker Corporation, MA, USA), scanning electron microscopy (SEM) analysis (Hitachi High Technologies, Tokyo, Japon), Fourier transform infrared spectroscopy (FTIR) analysis (Bruker Corporation, MA, USA) and atomic force microscopy (AFM) analysis was carried out using a Veeco (Plainview, NY, USA) (Figure 2, Figure 3, Figure 4, Figure 5, Figure 6, Figure 7, Figure 8, Figure 9 and Figure 10).

2.3. Adsorption Process

2.3.1. Adsorption Kinetics

The study of adsorption kinetics was carried out on barley seeds and biochar, operating under optimal conditions (pH 7 ± 0.3; adsorbent dose (0.01–0.02 mm) = 50 mg; dye concentration C₀ = 50 mg L⁻¹ stirring speed 150 rpm), the experiment matrix being adapted from other works [21]. In appropriate beakers, 50 mg of the adsorbent were mixed with 50 mL of the X-PR and MGC solution (C₀ = 50 mg L⁻¹). The suspension was stirred for 150 rpm at room temperature (21 °C). At previously defined time intervals (in the range of 0 to 120 min), the two adsorbents were separated from the liquid by centrifugation. The concentrations of the X-PR and MGC in the liquid phase were then determined by measuring the absorbance at 432 nm for X-PR and 617 nm for MGC following the reading on a calibration curve established from a range of X-PR and MGC concentrations from 0 to 50 mg·L⁻¹. The amount of X-PR and MGC (q_t) adsorbed by the two materials, as a function of time, was calculated according to the following formula:

$$q_e=\frac{\left(C_0-C_e\right)\ast V}{m}$$

(1)

$$R\%=\frac{\left(C_0-C_e\right)}{C_0}\ast 100$$

(2)

where C₀ is the concentration of the dye in (mg L⁻¹) in the liquid phase, V is the volume (L) of the dye solution and m is the mass of the adsorbent (g).

The four models tested are: the pseudo-first-order model developed by Lagergren in 1898 [22], which proposed a pseudo-first-order equation, Equation (3), in order to clarify the adsorption of the liquid/solid system. The second-order model is then given by the linear expression Equation (4) [23]. Then, the Elovich model can be expressed by the linear formula Equation (5) [24], and finally the intraparticle diffusion model is given by Equation (6) [25]:

$$\log \left(q_e-q_t\right)=\log \left(q_e\right)-\frac{K_{s1}}{2.303}t$$

(3)

$$\frac{t}{q_t}=\frac{t}{q_e}+\frac{1}{K_2{q}_e^2}$$

(4)

$$q_e=\frac{1}{\beta } ln\left(t\right)+\frac{1}{\beta } ln \left(\alpha \beta \right)$$

(5)

$$q_e=K_i \sqrt{t}+C$$

(6)

where:

• q_e is the amount adsorbed at equilibrium (mg g⁻¹),
• q_t is the quantity adsorbed at time t (mg g⁻¹),
• K_S1 is the rate constant of first order sorption (min⁻¹),
• K_i is the intraparticle diffusion rate constant,
• The value of the ordinate at the origin C provides an indication of the thickness of the boundary layer,
• K₂ (g mg⁻¹.min⁻¹) is the adsorption rate,
• α is the initial adsorption capacity (mg g⁻¹ min),
• β is the desorption constant (g mg⁻¹),
• t is the time (min).

2.3.2. Adsorption Isotherm

To obtain the adsorption isotherm, a series of beakers was used. Each beaker was filled with 50 mL of X-PR or MGC solution of varying concentrations: 0, 10, 20, 30, 40, 50, 60, 70, 80, 90 and 100 mg L⁻¹. The study of the adsorption equilibrium was carried out under the same optimal conditions indicated above. After equilibrium, the particles of the adsorbent were separated by centrifugation, and the clarified solution was analyzed by determination of the equilibrium concentration (C_e) of X-PR and MGC using the same calibration curve as previously used. The amount of reagent adsorbed at equilibrium (q_e, in mg g⁻¹) was calculated by Equation (1). To determine the adsorption isotherm, four adsorption modules were tested: the Langmuir model, Freundlich model, Temkin model and Dubinin–Radushkevich model. The most applicable model in the adsorption of X-PR by BS-HVL are the models of Langmuir and Freundlich. On the other hand, the Freundlich model is the most applicable in the elimination of MGC by BC-HVL. The adsorption of the Langmuir isotherm represented was attained from the following equation:

$$q_e=\frac{{\mathrm{q}}_{\mathrm{m} }{\mathrm{K}}_{\mathrm{L}}{C}_e}{1+{\mathrm{K}}_{\mathrm{L}}{C}_e}$$

(7)

This equation can be reshaped and rearranged into the following linear equation [26]:

$$\frac{C_e}{q_e}=\frac{C_e}{q_m}+\frac{1}{q_m{K}_L}$$

(8)

where q_e is the amount (mg g⁻¹) of X-PR and MGC adsorbed at equilibrium, C_e is the equilibrium concentration (mg L⁻¹), q_m is the monolayer adsorption capacity (mg g⁻¹) and K_L is the Langmuir constant (L mg⁻¹) related to the adsorption free energy.

An essential characteristic of the Langmuir isotherm can be expressed in terms of a dimension less constant called the separation factor and defined by the equation below [27,28]:

$$R_L=\frac{1}{1+K_L{C}_0}$$

(9)

where:

• C₀ is the initial concentration of the adsorbate (mg L⁻¹),
• K_L is the Langmuir constant (L mg⁻¹),
• R_L > 1 indicates that the adsorption is unfavorable,
• R_L = 1 indicates that the adsorption is linear,
• 0 < R_L < 1 indicates that the adsorption is favorable,
• R_L = 0 indicates that the adsorption is irreversible.

In our case, the found values of R_L are all between 0 and 1, which reveals favorable adsorption.

The linear form of Freundlich can be explained by the following equation:

$$\ln (q_e)=\ln \left(Kf+\frac{1}{n}\right)$$

(10)

The Slope of this line is 1/n which indicates adsorption intensity.

3. Results and Discussion

3.1. Interpretation of Analysis

The X-ray diffractograms of the BS-HVL and BC-HVL are shown in Figure 2 and Figure 3. Both materials show characteristic peaks at 2θ = 15°, 17°, 18°, 20° and 23° by diffraction of the (100), (020), (021), (110) and (200) planes of the hexagonal crystal lattice P31c(163) of sodium magnesium thiocyanate (Na₄Mg(SCN)₆) and crystals of magnesium iodide methanol (C₆H₂₄O₆MgI₂) and magnesium dodecanate (C₂₄H₄₆MgO₄) and characteristic peaks at 2θ = 13°, 15°, 25° and 28.5° by diffraction of the (0–12), (100), (024) and (0–15) planes of the triclinic crystal lattice P-1(2) and other crystal structure of calcium pyrazolone trihydrate (C₁₇H₁₃CaClN₄O₇S₂; 3H₂O) and 1,3-Distearoyl-2-Palmitoylglycerol (C₅₅H₁₀₆O₆) from the Triclinic P-1(2) crystal lattice. Most of the structure of BS-HVL and BC-HVL is amorphous, and the SEM might give a clear idea of the morphology of the investigated materials (Figure 5). This favors the adsorption of X-PR and MGC on both materials. The EDXA spectrum of BS-HVL (Figure 7a) also confirms the presence of a high percentage of carbon and oxygen in both materials, in addition to the presence of other elements such as K, P, Ca, Na and Si in BS-HVL. The EDXA spectrum of BC-HVL is shown in Figure 7b. After the adsorption of the X-PR and MGC dyes, the EDXA spectrum shows quite high percentages of carbon and oxygen, hence the fixation of both dyes inside the pores and on the surface of BS-HVL and BC-HVL. The SEM image also shows that the morphology of our material is modified after adsorption and the presence of the dye in the materials (Figure 6).

The images provided by the AFM analysis of the surface of the two materials give a clear idea that the surface of the seeds are rich with pillars (Figure 8a–c); on the other hand, biochar has a leash surface (Figure 8d). This difference between the natures of the surface can improve the adsorption capacity of the two colorants. Finally, the FTIR spectra of BS-HVL and BC-HVL were measured within the range of 500–4000 cm⁻¹ and are displayed in Figure 6, which shows OH⁻ functions associating phenol and alcohol from 3200 to 3400 cm⁻¹, C-H cycloalkane bonds from 2850 to 2925 cm⁻¹, phosphine from 2280 to 2410 cm⁻¹, N-H primary amines from 1550 to 1650 cm⁻¹, C=O carboxylic acid from 1400 to 1450 cm⁻¹, C-O primary alcohols from 1050 to 1080 cm⁻¹, C-O ethers from 1000 to 1090 cm⁻¹, Ar-C from 850 to 890 cm⁻¹ and, finally, monosubstituted aromatics from 700 to 800 cm⁻¹. After adsorption, the FTIR spectrum (Figure 10) shows the appearance of the new functions in the BC-HVL. This shows that the two biomaterials used to removal the X-PR and MGC are cost effective.

3.2. Effect of pH on the Adsorption Capacity of X-PR and MGC

According to Figure 11a, the effect of pH has a negative effect on the adsorption yield: when the pH increases, the yield decreases with the presence of H⁺ protons in the acidic medium and OH⁻ ions in the basic medium, which inhibits adsorption. Hydrogen and hydroxide ions are generally adsorbed quite strongly on the surface of the adsorbent. The number of active sites subsequently becomes small, and the adsorption of other ions becomes very difficult. Consequently, the adsorption of the two dyes decreases rapidly in the range from pH 2 to 8. For pH > 8, the decrease in adsorption becomes slower. On the other hand, for barley biochar BC-HVL (Figure 11b), the adsorption yield increases in the acidic medium because the level of H⁺ ions is very high and the charge transfer complexes are formed from weak interactions of donor and acceptor electrons that results in the formation of organometallic complexes in the environment.

3.3. Effect of the Adsorbent Dose on the Adsorption Capacity of X-PR and MGC

The study of the effect of the dose on the adsorption rate of the two dyes X-PR and MGC under experimental conditions is given by Figure 12a,b for the two materials BS-HVL and BC-HVL. The adsorption of the two dyes increases with the increase of the adsorbent dose during its range of study. This is due to the increased number of free sites on the adsorbent surface. The increase is quite large in the range of 0.01 to 0.07 g, but for adsorbent masses higher than 0.07 g, the variation becomes very small.

3.4. Effect of Initial Concentration

Figure 13 shows that when the dye concentration is increased, the adsorption efficiency of both dyes by both materials decreases [29,30]. The lowest dye removal was measured at an initial dye concentration from 10 to 100 mg L⁻¹ and the dye removal efficiency is higher at low concentrations between 10 and 60 mg L⁻¹, R% ≥ 86 for MGC and R% ≥ 56 for X-PR on BS-HVL and R% ≥ 20 for MGC and R% ≥ 18.5 for X-PR on BC-HVL. Therefore, the amounts adsorbed by BS-HVL are 9 to 94 mg g⁻¹ and 7 to 74 mg g⁻¹ for X-PR and MGC, respectively. Moreover, BC-HVL adsorbs 9.8 to 54 mg g⁻¹ and 8.6 to 91 mg g⁻¹ with X-PR and MGC, respectively.

3.5. Effect of Contact Time

The adsorption kinetics within 60 min are very important. This corresponds to a sufficient contact time that is able to eliminate the maximum amount of dye before reaching the chemical equilibrium point. For the time 60 ≤ t ≤ 80, the elimination speed becomes very low and reaches equilibrium, hence the ideal contact time for this experiment at equilibrium is 90 min (Figure 14). The dye adsorption rate of BS-HVL is much faster than that of BC-HVL. The maximum amounts adsorbed at t ≤ 60 min are 25 mg g⁻¹ and 28 mg g⁻¹ for BC-HVL and 42.5 mg g⁻¹ and 43 mg g⁻¹ for BS-HVL by X-PR and MGC, respectively.

3.6. Adsorption Kinetics

These results show that the most appropriate model for the adsorption of the two dyes is the pseudo-second-order model. Figure 15 and Figure 16 show the adsorption kinetics obtained in this study, and

Table 1. Adsorption kinetic constants of X-PR and MGC by BS-HVL (T = 21 ± 1 °C; m_ad = 50 mg; C₀ = 50 mg L⁻¹; stirring speed 150 rpm and pH = 7 ± 0.3).

Models		BS-HVL		BC-HVL
		X-PR	MGC	X-PR	MGC
Pseudo-first-order	R2	0.9179	0.9546	0.9127	0.9333
	K1 (min−1)	0.045	0.0565	0.0401	0.0551
	qe (mg g−1)	44.7817	72.3633	40.8007	66.4201
Pseudo-second-order	R2	0.9379	0.9969	0.9647	0.9692
	K2 (g mg−1 min−1)	0.0005	0.0011	0.0006	0.0007
	qe (mg g−1)	61.7283	54.0540	41.6667	41.8410
Elovich	R2	0.9101	0.9742	0.9429	0.9341
	α (mg g−1 min−1)	3.6528	7.8653	2.1251	2.6571
	β (g mg−1)	0.0674	0.0913	0.1071	0.1073
Intraparticle diffusion	R2	0.7969	0.9191	0.9519	0.9306
	Ki (mg g−1 min0.5)	4.2488	3.2554	2.8709	3.3419
	C (mg g−1)	5.3228	14.733	1.0959	3.3419

groups the results obtained by testing the four models.

3.7. Adsorption Isotherms

In this study, the models studied are the Langmuir model, Freundlich model, Temkin model, and Dubinin–Radushkevich model. The most frequently established model for the study from the adsorption isotherms is the Langmuir model (Figure 17a–d); the results obtained are shown in

Table 2. Adsorption isotherms constants of X-PR and MGC on BS-HVL and BC-HVL (T = 21 ± 1 °C; t = 90 min, m_ad = 50 mg; stirring speed 150 rpm and pH = 7± 0.3).

Models	Constants	BS-HVL		BC-HVL
		X-PR	MGC	X-PR	MGC
Langmuir	R2	0.9954	0.8953	0.6271	0.8954
	RL	0.1862–0.6958	0.0089–0.0823	0.0405–0.2968	0.0099–0.9091
	KL (L mg−1)	0.0437	1.115	0.2369	1
	qm (mg g−1)	71.642	50	44.843	121.95
Freundlich	R2	0.9954	0.977	0.7529	0.9927
	KF (L mg−1)	4.4017	5.1908	13.5637	6.2883
	n	0.9975	0.9876	3.5385	0.8011
Temkin	R2	0.8793	0.9195	0.5801	0.9441
	KT (L mg−1)	0.1074	0.1117	0.1104	0.6773
	B1 (J mol−1)	7.498	6.427	6.6877	45.011
	b	325.3889	380.1369	365.3184	54.2787
Dubinin– Radushkevich	R2	0.6943	0.7648	0.4148	0.8968
	Kad (mol2 KJ−2)	20 × 10−5	30 × 10−5	0.04 × 10−5	1 × 10−5
	E (KJ mol−1)	15.8114	12.9099	35.3563	70.7108
	qm (mg g−1)	11.5802	10.7124	31.5004	71.715

.

3.8. Statistical Analysis

The results are reported as the means of four replicates. The data obtained were subjected to one-way analysis of variance (ANOVA) for assessing the significance of quantitative changes in the variables as a result of biochar treatments. The statistical analysis was done by the Statistical Package for Social Science (IBM SPSS Statistics 23.0, Chicago, IL, USA)

According to the statistical analysis (

Table 3. Analysis of variance (F-test) of the effects on the adsorption of X-PR and MGC in the two biomaterials BS-HVL and BC-HVL.

Type of Analysis	Parameter Study	Type of Sample	Mean	Std. Error	95% Confidence Interval		Test ANOVA
					Lower Bound	Upper Bound	F	Sig.
Effect of pH on the adsorption capacity of X-PR and MGC	Adsorption capacity, X-PR, (mg g−1)	BS-HVL	30.737	2.244	24.966	36.5080	19.735	0.001 S
		BC-HVL	14.918	2.764	7.812	22.023
	Adsorption capacity, MGC, (mg g−1)	BS-HVL	22.690	4.104	12.139	33.241	1.784	0.211 NS
		BC-HVL	16.011	2.855	8.670	23.353
Effect of adsorbent dose on adsorption yield of X-PR and MGC	Adsorption yield, X-PR, (%)	BS-HVL	46.300	5.621	33.58	59.02	0.360	0.556 NS
		BC-HVL	42.100	4.165	32.68	51.52
	Adsorption yield, MGC, (%)	BS-HVL	63.300	8.013	45.17	81.43	0.034	0.855 NS
		BC-HVL	61.200	8.023	43.05	79.35
Effect of concentration on the adsorption capacity of X-PR and MGC	Adsorption capacity, X-PR, (mg g−1)	BS-HVL	51.578	9.270	22.284	80.871	3.537	0.076 NS
		BC-HVL	31.897	4.872	16.498	47.295
	Adsorption capacity, MGC, (mg g−1)	BS-HVL	46.072	7.715	21.691	70.452	0.105	0.749 NS
		BC-HVL	49.859	8.774	22.131	77.587
Effect of contact time on adsorption capacity of X-PR and MGC	Adsorption capacity, X-PR, (mg g−1)	BS-HVL	37.920	3.669	26.323	49.517	13.670	0.001 S
		BC-HVL	23.250	2.333	15.875	30.625
	Adsorption capacity, MGC, (mg g−1)	BS-HVL	39.750	2.655	31.358	48.142	20.278	0.000 S
		BC-HVL	25.33	2.330	17.965	32.695
Effect of temperature on adsorption of X-PR and MGC	Adsorption capacity, X-PR, (mg g−1)	BS-HVL	43.02	1.098	39.548	46.492	13.003	0.011 S
		BC-HVL	49.3135	0.10	48.966	49.660
	Adsorption capacity, MGC, (mg g−1)	BS-HVL	32.87	1.158	29.210	36.530	75.522	0.000 S
		BC-HVL	48.8510	0.115	48.484	49.217

Values are averages ± standard deviation of triplicate analysis. Data obtained were subjected to one-way analysis of variance (ANOVA). NS: nonsignificant (p > 0.05); S: significant (p < 0.05).

) of the effect of pH on the adsorption capacity, there is a significant difference (p < 0.05) between the means of the adsorption capacities of X-PR by the two materials BS-HVL and BC-HVL; on the other hand, there is no significant difference (p = 0.211) between the means of the adsorption capacities of MGC by the two studied materials (BS-HVL and BC-HVL). Furthermore, the statistical analysis of the effect of the dose shows that there is no significant difference (p > 0.05) between the means of the adsorption capacities of X-PR and MGC by the two materials BS-HVL and BC-HVL. On the one hand, the statistical analysis of the effect of the initial concentration shows that the test is insignificant at the 5% level, with no significant difference between the means of the adsorption capacities of X-PR and MGC by the two materials BS-HVL and BC-HVL. On the other hand, the statistical analysis of the effect of contact time shows that the test is highly significant at the 1% value; there is a significant difference between the mean adsorption capacities of X-PR and MGC by the two materials BS-HVL and BC-HVL. Moreover, the statistical analysis of the effect of temperature shows a highly significant test at the 5% threshold, indicating that there is a significant difference between the means of adsorption capacities of X-PR and MGC by the two materials BS-HVL and BC-HVL.

3.9. Comparison of Adsorption Capacity with Various Adsorbents

Table 4. The adsorption capacity of dyes and heavy metals in aqueous solutions by activated carbons of different biomass.

Adsorbate	Adsorbent Pollutants	Dose (mg)	C0 (mg L−1)	pH	Kinetic	Isotherm	qm (mg g−1)	Ref.
Zinc oxide loaded activated char (ZnO-AC)	OG Rh-b	8–30	50	7	Pseudo-second-order	Langmuir	153.8 128.2	[5]
Rice straw (RS) biochar Wood chip (WC) biochar	CV-CR	01	500	7	Pseudo-second-order	Langmuir	620.3 195.6	[31]
Charcoal (tree branches) (BCA-TiO2)	MB Cd2+	** **	0.4 600	7 8	Pseudo-second-order	**	200 250	[32]
Sulfonated peanut shell (PNS-SO3H)	MB TC	20	900 ppm	10	Pseudo-second-order	Langmuir	1250 303	[33,34]
Shrimp shell (SS) Coal acid mine drainage (AMD)	Mn Fe	**	≤1 ≤15	6–9 5–9	Pseudo-second-order	Frendlich	17.43 3.87	[35]
Coal fly ash (CFA)	MG RG	40 30	100 ppm	8	Pseudo-second-order	Langmuir	233.3 381.7	[36]
Biomass CLS Biochar (BCCLS)	RR-23	50	50	7	Pseudo-second-order	Langmuir	62.5 166.67	[37]
Biomass CLSh Biochar (BCCLSh)	RR-23	50	50	7	Pseudo-second-order	Langmuir	90.91 354.82	[24]
Biochar BC CLS Biochar (BCCLSh)	AO-52	50	300	7	Pseudo-second-order	Langmuir	333.33 500	[22]
Silica-Chitosan Composite	RR-23 RB19	40	60	7	Pseudo-second-order	Langmuir	128.2 156.25	[38]
Chitosan Composite MCs/MS	RR-23 RB19 Fe2+	70	50	7	Pseudo-second-order	Langmuir Frendlich Frendlich	71.94 175.44 62.11	[23]
Activated Carbon derived from Phragmites Australis	MO MV	50 50	500 400	**	Pseudo-second-order	Langmuir	238.11 476.19	[39]
Carbon nanotubes (CNTs)	MO	200 mg L−1	10	**	Pseudo-second-order	Langmuir	55.2	[40]
Carbon of Quercus Brantii (Oak)	ACT IBP	1 g L−1	100	7	Pseudo-second-order	Freundlich	45.45 96.15	[41]
BS−HVL	X−PR	50	50	7	Pseudo-second-order	Langmuir-Freundlich	71.642	This work
BS−HVL	MGC	50	50	7	Pseudo-second-order	Freundlich	44.843
BS−HVL	X−PR	50	50	7	Pseudo-second-order	Freundlich	44.843
BS−HVL	MGC	50	50	7	Pseudo-second-order	Freundlich	121.95

** undetermined.

shows the adsorption capacity of dyes and heavy metals in aqueous solutions by activated carbons of different biomass. The majority of the activated carbons used in the removal of the anionic dyes, cationic dyes and heavy metals have adsorbed quantities of less than 500 mg g⁻¹, except that Rice straw charcoal has an adsorbed quantity equal to 620 mg g⁻¹.

3.10. Adsorption Thermodynamics Studies

The thermodynamic parameters, such as the Gibbs free energy change (ΔG°), enthalpy (ΔH°) and entropy (ΔS°), were calculated using the following equations [42]:

$$K=\frac{Q_{e }}{C_e}$$

(11)

The value of ΔG° can be determined from the following equation:

$$\mathsf{\Delta }G°=-RT ln\left(K\right)$$

(12)

where K is the thermodynamic equilibrium constant.

The effect of temperature on thermodynamic constant is determined by the following equation:

$$\frac{\mathrm{d}\left(\ln \left(\mathrm{K}\right)\right)}{\mathrm{dt}}=\frac{\mathsf{\Delta }{H}^{°}}{R{T}^2}$$

(13)

Integrating and rearranging Equation (14), we obtain

$$ln \left(K\right)=\frac{\mathsf{\Delta }S°}{R}-\frac{\mathsf{\Delta }H°}{RT}$$

(14)

Additionally, Gibbs free energy is also given by

$$\mathsf{\Delta }G°=\mathsf{\Delta }H°-T\mathsf{\Delta }S°$$

(15)

The ∆H° and ∆S° values were calculated from the slope and intercept of the linear plot of ln(K) versus 1/T. Such parameters reflect the feasibility and spontaneous nature of the process [43]. Experiments were carried out using 50 mg L⁻¹ dye solutions with 50 mg of BC-HVL or BS-HVL for 90 min at different temperatures. The apparent equilibrium constant K of the adsorption is calculated by Equation (10). The free energy of Gibbs of the adsorption ΔG° is calculated from Equation (11), the relationship between K and the temperature is given by the Van ’t Hoff equation [44] and the enthalpy and entropy can be gained from the slope and the interception of the Van ’t Hoff plot of ln(K) with respect to 1/T, which are shown in Figure 18.

The Temkin isotherm equation is

$$q_e=B_1 ln KT+B_1 ln\left(C_e\right)$$

(16)

The Dubinin–Radushkevich isotherm is expressed as follows:

$$ln\left(q\right)=ln(q_0)-K{E}^2$$

(17)

$$\mathsf{\epsilon } = \mathrm{RT} \ln \left(1+\frac{1}{C_e}\right)$$

(18)

where ε is the Polanyi potential, K is the Dubinin–Radushkevich constant, R is the gas constant (8.31 Jmol⁻¹ k⁻¹), T is the absolute temperature and E is the mean adsorption energy.

In order to determine the thermodynamic parameters, the sorption studies were carried out at various temperatures (294, 303, 323 and 343 K). The values of ΔH° and ΔS° were calculated from the slope and intercept of plot between ΔG° vs. T. The calculated values of ΔH°, ΔS° and ΔG° are listed in

Table 5. Thermodynamic parameters for the adsorption of X-PR and MGC onto BS-HVL and BC-HVL (m_ad = 50 mg; C₀ = 50 mg L⁻¹; pH = 7 ± 0.3 and stirring speed 150 rpm).

Parameters		BS-HVL		BC-HVL
		X-PR	MGC	X-PR	MGC
ΔH° (kJ mol−1)		23.55	12.757	21.179	13.386
ΔS° (J mol−1 K−1)		90.797	46.074	103.734	74.759
ΔG° (kJ mol−1)	T = 294 K	−27.034	−13.533	−30.477	−21.966
	T= 303 K	−27.942	−13.948	−31.410	−22.639
	T= 323 K	−29.758	−14.869	−33.485	−24.134
	T= 343 K	−30.666	−15.791	−35.560	−25.629

. The negative free energy changes (ΔG°) at all the studied temperatures proposed that the adsorption of X-PR and MGC onto the BS-HVL and BC-HVL adsorbents was feasible and spontaneous thermodynamically. This shows an increased randomness at the solid solution interface throughout the fixation of the dye on the active sites of the adsorbent. The positive value of ΔH° further reveals that the adsorption is an endothermic process, demonstrating that the adsorption process decreases with an increase in temperature. The positive value of ΔS° infers that X-PR and MGC in the bulk phase (aqueous solution) were in a much more chaotic distribution in comparison to the relatively ordered state of the solid phase (surface of adsorbent). Additionally, the positive value of ΔS° represents a result of the affinity of the adsorbent for the two dyes.

4. Conclusions

In this work, we studied the possibility of using coproducts of plant origin as adsorbent systems for environmental pollutants. These materials are the starch-enriched and deproteinized barley seeds BS-HVL and BC-HVL. There are several reasons for using these materials. First, they may be used for the development of natural materials for specific applications in water depollution. The majority of organic flocculants, coagulants and adsorbents used in the field of water treatment are obtained from synthetic (petroleum) resources. The seeds we modified are abundant and cheap products, made from renewable, biodegradable and biocompatible agricultural raw materials. The second reason is in line with the development of sustainable chemistry. The BS-HVL and BC-HVL that were used are deproteinized fractions enriched with starch, a polysaccharide which presents very interesting modification chemistry. To simplify the optimization process, the effect of pH was first studied by a one-variable-at-a-time method, after which the influences of other parameters, such as sonication time, initial dye concentrations and adsorbent dosage were examined. The optimal conditions were pH 7, a dose of 0.05 g of BC-HVL or BS-HVL, a sonication time of 90 min, and initial concentrations of 50 mg L⁻¹ for X-PR and MGC, respectively, which resulted in high removal percentages (91% for X-PR and 98% for MGC). In addition, the adsorption capacities were 71.6 mg g⁻¹ and 44.8 mg g⁻¹ for X-PR and 44.8 mg g⁻¹ and 121.5 mg g⁻¹ for MGC. The adsorption equilibrium study showed that both Langmuir and Freundlich models had adequate competence for the description and evaluation of the adsorption process. The kinetic study was performed at different time intervals. The results indicated that the adsorption processes can be fitted and predicted by the pseudo-second-order model with an adsorption capacity of 61.7 mg g⁻¹ and 41.7 mg g⁻¹ for X-PR and 54 mg g⁻¹ and 41.8 mg g⁻¹ for MGC. In a difficult economic context, characterized by increased competition on the polysaccharide market, cereal producers are wondering about the possibilities of novel applications for the products and wastes from this sector of activity.