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Environ Eng Res > Volume 25(4); 2020 > Article
Ren, Chen, Wang, Song, Zhou, and Ren: Magnetic biochar from alkali-activated rice straw for removal of rhodamine B from aqueous solution

Abstract

To address organic dye wastewater, economic and effective adsorbents are required. Here, magnetic biochar from alkali-activated rice straw (AMBC) was successfully synthesized using one-step magnetization and carbonization method. The alkaline activation caused the large specific surface area, high pore volume and abundant oxygen-containing groups of the AMBC, and the magnetization gave the AMBC a certain degree of electropositivity and fast equilibrium characteristics. These characteristics collectively contributed to a relative high adsorption capacity of 53.66 mg g−1 for this adsorbent towards rhodamine B (RhB). In brief, RhB can spontaneously adsorb onto the heterogeneous surface of the AMBC and reach the equilibrium in 60 min. Although the initial pH, ionic strength and other substances of the solution affected the adsorption performance of the AMBC, it could be easily regenerated and reused with considerable adsorption content. Based on the results, H-bonds, π–π stacking and electrostatic interactions were speculated as the primary mechanisms for RhB adsorption onto the AMBC, which was also demonstrated by the FTIR analysis. With the advantageous features of low cost, easy separation, considerable adsorption capacity and favorable stability and reusability, the AMBC would be a potential adsorbent for removing organic dyes from wastewater.

1. Introduction

With the rapid development of industry, more than one million tons of organic dyes are manufactured worldwide every year, and releasing of the dyes into natural waters is mostly through industrial effluents [1]. The discharged organic dyes have caused serious water pollution, and posed threat to the health of aquatic ecosystems and human beings [2, 3]. Rhodamine B (RhB), as one of the organic dyes, is widely used to impart color to paper, textile, leather, printing, food and other products. Subsequently, RhB may be released into the environment. As reported by previous studies, RhB is resistant to natural degradation, and can exert serious carcinogenicity, reproductive toxicity and neurotoxicity to animal [4, 5]. Therefore, it is essential to remove RhB from wastewaters.
In recent years, various separation and transformation technologies such as adsorption, biological degradation and photolysis were developed to treat the organic dye wastewaters. Compared to other methods, adsorption has the advantages of time-saving, low cost, simple design and low energy consumption. Adsorption has been used to separate organic dyes from wastewaters, but traditional adsorbents limit its application at a large scale. For this reason, considerable efforts have been devoted by researchers to develop novel adsorbents. A large number of emerging materials, including biochar (BC), graphene oxide and multi-walled carbon nanotubes, are fabricated and applied for adsorption of organic dyes [68]. Among these materials, BC has been known as an innovative and promising adsorbent due to its numerous functional groups, good stability, high surface area, low cost, and easily accessible characteristics [9, 10]. However, due to poor separation and regeneration of BC, its application in wastewater treatment is very limited [11]. Furthermore, the BC released into natural waters may cause the secondary pollution by enhancing the migration and resuspension of pollutants in the sediments. Thus, synthesis of BC-based adsorbents overcoming those shortcomings is critical for its further industrial application.
Introduction of magnetic nanoparticles can remarkably overcome the disadvantage of BC with respect to separation from solutions. Fe3O4 particles, feature merits in strongly magnetic properties, were previously loaded onto BC using several methods, including co-precipitation, hydrothermal reaction and microwave irradiation [7, 12, 13]. The composite prepared by co-precipitation is usually unstable under acidic condition, and hydrothermal and microwave reactions are time- and energy-consuming. Furthermore, magnetization and carbonization are two traditionally independent procedures for magnetic BC preparation. In recent years, the two processes were successfully incorporated into one step to cut the time and energy costs [14, 15]. However, the adsorption performance of BC was sacrificed on a large scale due to the negative effects of magnetic particles. As reported previously, metal hydroxide coating and alkaline activation could effectively promote the adsorption performance of BC [1618]. On this basis, we hypothesize that the introduction of alkaline activation procedure into magnetic BC synthesis may eliminate the negative effects from magnetization. To date, the information is still very limited on the preparation and application of the BC derived from alkali-activated biomass using one-step carbonization and magnetization method.
Herein, alkali-activated rice straw was used to synthesize the magnetic biochar (AMBC) by a facile method. The adsorption capacity, behavior and mechanisms of this material were systematically studied using RhB as a model organic dye. The influence of some aquatic environment factors such as pH and ionic strength was also explored on the adsorption of RhB to the AMBC. Finally, regeneration and reusability of the adsorbent were studied. The present study provides new insights into developing BC and advances its application in wastewater treatment.

2. Material and Methods

2.1. Chemicals

RhB was purchased from Sigma-Aldrich at a purity of 95%. Sodium hydroxide (NaOH), hydrochloric acid (HCl), nitric acid (HNO3), hydrogen fluoride (HF), hydrogen peroxide (H2O2), sodium chloride (NaCl), calcium chloride (CaCl2) and ferric chloride hexahydrate (FeCl3·6H2O) were purchased in analytical grade from Sinopharm Chemical Reagent Co., Ltd., China. All the chemicals were used as received without further purification. Ultrapure water (18.2 MΩ cm, 25°C) was prepared by a Milli-Q system in the laboratory.

2.2. Adsorbents Synthesis

Rice straws were collected from a cropland in Cangxi county October 2018, Sichuan province, China. The samples were cleaned and washed with tap water, air dried for four weeks and then chopped to pass through 10 mesh sieve.
The AMBC was synthesized using a method previously described with some modifications [14], as shown in Fig. S1. In brief, 50 g of the raw material was soaked in 500 mL of NaOH solution (0.2 mol L−1) for one hour. The alkali-activated straws were washed and then dispersed in 500 mL of FeCl3 solution (1.0 mol L−1) followed by heated at 50°C for another 30 min. After that, the Fe3+ loaded straws were separated and washed three times with ultrapure water. Finally, the modified straws were pyrolyzed at 650°C for 60 min under N2 atmosphere (200 mL min−1). The pyrolysis temperature was optimized by collectively considering the adsorption performance, magnetism strength and energy consumption of the AMBC. For comparison, BC was obtained by pyrolysis the raw straws with the same conditions, and magnetic biochar (MBC) was prepared by pyrolysis the Fe3+ loaded rice straw without alkaline activation.

2.3. Material Characterization

Composition of C, H, O and N of the AMBC was analyzed by an elemental analyzer (Elementar, Germany). For iron quantification, the AMBC was digested with HNO3–H2O2–HF, and determined by an inductively coupled plasma atomic emission spectrophotometry (Agilent 7700s). The magnetic property was characterized on a vibrating sample magnetometer at room temperature (MPMS XL-5). The pH of zero point charge (pHPZC) was determined using a previously reported method [19]. The prepared BC and MBC were also characterized using the same methods to obtain their physicochemical properties.
The morphology of the ABMC was obtained using scanning electron microscopy (Zeiss Sigma 500). Briefly, 10 mg of each adsorbent was dispersed in 20 mL pure water for 30 min and then picked up onto a carbon-coated copper grid. After being dried, the adsorbents were photographed under high vacuum at 30 kV voltages. The Brunauer–Emmett–Teller (BET) method (ASAP 2460) was used to analyze the specific surface area, pore volume and pore diameter by nitrogen adsorption–desorption isotherm. Prior to measurement, the AMBC was outgassed at 300°C for 4 h. Functional groups in the adsorbent were analyzed on a Fourier transform infrared (FTIR) spectroscopy (Varian 640) using a potassium bromide pellets technique [20].

2.4. Adsorption Experiments

Batch adsorption experiments were carried out in 40-mL glass vials with Teflon-lined caps in triplicate. To this end, the effects of contact time and initial concentration were pre-assessed on RhB removal. The adsorption kinetics of RhB was studied at 25°C with shaking at 180 rpm. Briefly, 40 mg of the AMBC was added into 40 mL of RhB solution (50 mg L−1, pH = 6.5 ± 0.2), and the samples were taken at selected time intervals for RhB quantification. The adsorption isotherms were obtained with RhB ranging from 10 to 100 mg L−1 at 10, 25 and 40°C, respectively.
To explore the influence of pH on RhB adsorption onto the AMBC, the solutions were adjusted to a pH range of 2–11 using 2.0 mol L−1 NaOH and HCl. The effect of ionic strength on RhB adsorption was investigated from 0.05 to 0.5 adjusted by NaCl and CaCl2 at pH = 6.5. Temperature for all the experiments was controlled at 25°C, and the concentration of RhB was 50 mg L−1. After adsorption equilibrium, samples were collected for RhB quantification. All of the experiments were performed in triplicate.

2.5. Stability and Reusability of the AMBC

The stability and reusability of the AMBC were evaluated by the cycle number-dependent removal rate of RhB, and a total of 3 cycles were carried out. Briefly, the adsorption performance was tested by mixing 40 mg of the AMBC with 40 mL of RhB solution (50 mg L−1) at pH = 6.5. After a 60 min shaking at room temperature, the AMBC was recovered using a magnet. It was then dispersed in 40 mL methanol-water solution (v/v, 7:3) and sonicated for 10 min. After that, the regenerated adsorbents were magnetically separated from the solution, washed thoroughly with ultrapure water, vacuum dried and used for subsequent adsorption. To further evaluate the regeneration and reusability of the AMBC in practical application, the cycle number-dependent removal rate of RhB was determined in a model textile effluent synthetized according to the OECD guidelines. Briefly, the synthetic wastewater was consisted by (per liter of tap water): 160 mg of peptone, 110 mg of meat extract, 30 mg of urea, 28 mg of K2HPO4, 7 mg of NaCl, 4 mg of CaCl2·2H2O, 2 mg of MgSO4·7H2O and 50 mg of RhB.

2.6. RhB Quantification

The absorbance of RhB in the solutions was determined by an UV–vis spectrometer (UV-2600, Shimadzu) at a wavelength of 554 nm. The concentration of RhB was calculated using a correction curve with an adjusted R2 > 0.999 in 0.2–20 mg L−1 (Fig. S2). The amount of RhB adsorbed by the adsorbents at time t and equilibrium was calculated using the Eq. (1) and (2).
(1)
qt=(Co-Ct)×V/m
(2)
qe=(Co-Ce)×V/m
where C0, Ce, and Ct (mg L−1) are the initial concentration, equilibrium concentration, and concentration of RhB at time t (min), respectively. m is the mass of the adsorbent (g), and V is the volume of the solution (L).

2.7. Data Analysis

Pseudo-first and -second order kinetic models, shown as Eq. (3) and (4), were used to describe the adsorption mechanisms of RhB. In addition, a diffusion model as Eq. (5) was applied to evaluate the influence of diffusion process on the adsorption kinetics.
(3)
qt=qe(1-e-k1t)
(4)
qt=qe2k2t(1+qek2t)-1
(5)
qt=qekt1/2+C
where qt (mg g−1) is the adsorption amount at time t (min), and qe (mg g−1) is the adsorption capacity at equilibrium. k1 (min−1), k2 (g mg−1 min−1) and k (g mg−1 min−0.5) are the rate constants. C is a constant for the intra-particle diffusion model.
The adsorption isotherms were descried using Freundlich and Langmuir models, as Eq. (6) and (7).
(6)
qe=KFCe1/n
(7)
qe=qmaxKLCe(1+KLCe)-1
where qe is defined to be the same as above, and Ce is the RhB equilibrium concentration (mg L−1); qmax (mg g−1) is the maximum adsorption capacity; 1/n is an empirical constant of the Freundlich model; KF ((mg g−1) (mg L−1)n) and KL (L mg−1) are the Freundlich and Langmuir adsorption affinity parameter, respectively.
The thermodynamic parameters including standard free energy change (ΔG0), entropy change (ΔS0) and enthalpy change (ΔH0) were calculated using Eq. (8) and (9).
(8)
ΔGo=-RTln Ko
(9)
ΔHo=TΔSo-RTln Ko
where R (8.314 J mol−1 K−1) is the universal gas constant, and T (K) is the thermodynamic temperature for the systems. K0 is the adsorption equilibrium constant.

3. Results and Discussion

3.1. Characteristics of the Adsorbents

The AMBC possessed abundant cracks and porosity on its surface (Fig. 1(a) and (b)). The isotherms (Fig. 1(c)) were determined as type IV for the AMBC, which was the characteristics of mesoporous material and the reason for the significant volume of nitrogen adsorbed at relative high pressure [14, 21]. The specific surface area was measured as 396.9 m2 g−1 for the AMBC, about 2.0 and 1.4 times larger than that of the BC and MBC (Table S1). According to the result of dynamic light scattering analysis, about 34.41%, 54.76% and 10.94% of the AMBCs were 250–400 nm, 400–550 nm and 550–850 nm, and the average particle size was 466.87 nm (Fig. 1(d)). The energy dispersive spectroscopy analysis confirmed that iron was successfully introduced into the biochar (Fig. 1(e)). The iron content of the AMBC was quantified as 37.49 mg g−1, and most of the iron formed the magnetic composition because the AMBC has strong magnetism about 3.12 emu g−1, as shown in Fig. S3.
The C, H, O, N and S contents of the AMBC were 76.48%, 2.67%, 16.20%, 0.16% and 0.08%, respectively, which was similar to the composition of BCs reported by other researchers [22]. Compared to the BC and MBC, the carbon content of the AMBC was slightly lower, but the oxygen content was higher (Table S1). This result could be explained by the enhanced release of carbonaceous volatiles due to the magnetization and alkaline activation used in the preparation processes.
The pHpzc of the BC was significantly changed by the treatments of alkaline activation and magnetization (Fig. S4). The pHpzc of maghemite mainly comprised by FeOH2+ was reported to be 6.5 or higher [23]. Thus, the increased pHpzc for the MBC and AMBC, compared to the BC, was primarily derived from the magnetization process. Based on the result of the elemental analysis, alkaline activation introduced of more oxygen-containing groups, which would contribute to the lower pHpzc of the AMBC than the MBC. These results collectively indicated that the AMBC was successfully synthesized from the alkali-activated rice straws using one-step magnetization and carbonization method.

3.2. RhB Adsorption Kinetics

To explore the adsorption rate of RhB onto the AMBC and the time required for reaching adsorption equilibrium, adsorption kinetics were investigated. As shown in Fig. 2(a), a rapid adsorption of RhB onto the AMBC occurred during the first 5 min, and the adsorption capacity reached about 90% of its maximum. After that, a slow process until adsorption equilibrium was reached about 60 min. Similarly, magnetic biochar was also determined to reach equilibrium more rapid than BCs in adsorption of 17β-estradiol, hexavalent chromium and other pollutants [14, 24]. Based on the results, 60 min was chosen as the contact time to achieve equilibrium for the further adsorption studies. Compared to the adsorption performance of magnetic active carbon, carbon nanotubes and other carbon materials [2527], the time required for reaching adsorption equilibrium was much shorter for the AMBC. This might be assigned to the porous structures on this material, enabling easy and fast access of RhB to the adsorption sites [28].
The adsorption process was further analyzed using pseudo-first and -second order models as Eq. (3) and (4). The pseudo-second order model can describe the adsorption of RhB onto the AMBC more precisely with relatively higher adjusted determination coefficient ( RAdj2), as listed in Table S2. It indicated that the chemical adsorption would be the rate-limiting mechanism for RhB adsorption onto the adsorbent. It is interesting that the pseudo-second order model was also suitable for describing the adsorption of RhB onto the BC and MBC (Fig. S5), meaning that the alkaline activation and magnetization did not change the adsorption kinetics pattern. Similar results were also reported by previous studies performed to explore the feasibility of using BC and magnetic BC derived from biomass to remove organic pollutants from aqueous solution [29, 30]. For pseudo-second order model, the initial adsorption rate r (mg (g min)−1) is proportion to the adsorption equilibrium capacity and can be calculated using the equation as r=k2qe2 [31]. The value of r for the AMBC was much higher than that of the BC but lower than that of the MBC (Table S2). Thus, the magnetization was the primary driving force for the fast mass transfer of RhB from bulk solution onto the AMBC.
Intra-particle diffusion model as Eq. (5) was fitted to identify the mass transfer resistance for RhB adsorption onto the AMBC. If the value of C in the model equals zero, the adsorption rate is controlled by intra-particle diffusion for the whole process [32]. As shown in Fig. 2(b), the adsorption of RhB onto the AMBC was comprised by three stages. The first sharper slope represents the film diffusion process for RhB from bulk solution to the AMBC surface. The second part is the result of the intra-particle diffusion of RhB. The last part is the equilibrium stage, i.e., the adsorption of RhB onto the internal surface of the adsorbent. Therefore, intra-particle diffusion was present as one part of RhB adsorption onto the AMBC, but it was not the rate-limiting step for the whole process. Due to failure to obtain the data of the fast diffusion phase, two parts were fitted for the adsorption process of RhB onto the MBC (Fig. S6). However, the whole adsorption process would be still comprised by three stages because the intercept of the first fitted stage was about 30 mg g−1. It should be noted that the diffusion and adsorption of RhB onto the BC (Fig. S6) were distinctively different from that onto the MBC and AMBC. These results demonstrated that the alkaline activation and magnetization indeed altered the mass transfer mechanisms for RhB adsorption onto the BC.

3.3. RhB Adsorption Isotherms

The adsorption isotherms of RhB at different temperatures to the AMBC are displayed in Fig. 3, and the fitted parameters are listed in Table 1. The adsorption isotherms can provide insights into the distribution characteristics of adsorbates to the adsorbents. The Langmuir model assumes that pollutant adsorbs as monolayer onto a homogeneous surface, while the Freundlich model was derived on an exactly opposite position [33]. In this study, the Freundlich model was superior than the Langmuir model in describing the adsorption behaviors of RhB onto the AMBC based on the adjusted R2 values. It indicated the diversity of adsorption sites on the adsorbent. Similar phenomena were found for the adsorption of RhB to the MBC and BC (Fig. S7). Therefore, the three adsorbents had similar adsorption thermodynamic characteristics toward RhB.
The adsorption capacity of the AMBC towards RhB increased with the increment of RhB concentration and reaction temperature. Specifically, KF was calculated as 12.56, 16.28 and 17.68 at 10, 25 and 40°C, respectively. Similar results were also reported by other researchers when studying the adsorption performance of the pristine and modified biochars [34, 35].
Although similar thermodynamic behaviors were found for the MBC and BC (Table S3), the maximum adsorption capacity of the MBC and BC towards RhB was much lower than that of the AMBC. It demonstrated that alkaline activation was primarily responsible for the enhancement of the adsorption capacity. Compared to the BCs pyrolyzed from other biomass such as earthworm manure, corn straw and Pongamia glabra seed cover [6, 36, 37], the AMBC also exhibited an excellent adsorption performance. Therefore, the alkaline activation is indeed responsible for the high adsorption capacity of the AMBC, which might be attributed to its large specific surface area, abundant porous structure and specific reaction sites.
The thermodynamic parameters for the adsorption of RhB onto the AMBC were calculated, and the results were shown in Table 2. The ΔG0 was negative for the AMBC at all the temperatures, indicating that the adsorption processes were spontaneous. With temperature increasing from 10°C to 40°C, the ΔG0 values gradually decreased, meaning that the higher temperature could facilitate the adsorption of RhB onto the AMBC. Similar trend was also found with the BC (Table S4), but the values were significantly lower than that of the AMBC. It was the reason why the adsorption capacities of the BC and MBC smaller than that of the AMBC. The positive values of ΔH0 indicated that the adsorption of RhB onto the AMBC was an endothermic process. This was the reason why the adsorption capacity increased with the enhancement of the reaction temperature. The positive values of ΔS0 represented the increased randomness at the interfaces in the adsorption progress. These behaviors of RhB adsorption to the AMBC agreed with the adsorption of Pb2+, Congo red, Titan yellow and other pollutants onto the biomass-derived MBC [38, 39].

3.4. RhB Adsorption Affected by Hydro-Chemical Factors

3.4.1. Influence of pH

pH is one of the important factors affecting the adsorption process in liquid phase, which can markedly change the speciation of the adsorbates and the surficial properties of the adsorbents. In this study, the adsorption capacity of the AMBC was first increased with pH increased from 2.0 to 4.0, and then decreased with pH further increasing (Fig. 4(a)). Thus, the pH condition of 4.0 is conducive to remove RhB from wastewater by this material. This phenomenon might be caused by the variation of the surface charge of the AMBC and the speciation of RhB at different pH levels. In terms of the detected pHzpc, the surface of the AMBC is positively charged at pH < 4.4 and negatively charged at pH > 4.4. With a dissociation constant pKa of 3.7 [40], RhB molecules exist predominantly in cationic form at pH < 3.0 and in zwitterion form at pH > 5.0. The electrostatic attraction might contribute to the maximum sorption capacity of the AMBC at pH = 4.0, and the electrostatic repulsion would hinder RhB adsorption onto the surface of the AMBC under the strong acidic and alkaline conditions. It should be noted that the surface oxygen containing groups of the AMBC could also contribute to its excellent adsorption affinity with RhB by forming H-bonds. Thus, the breaking of the H-bonds would also reduce the adsorption of RhB onto the AMBC under alkaline conditions.

3.4.2. Influence of ionic strength

High content of salts in solutions is known to affect the adsorption of chemicals to adsorbents. In this study, NaCl and CaCl2 were used to evaluate the influence of ionic strength on the uptake of RhB by the AMBC. It can be seen from Fig. 4(b), the adsorption of RhB onto the adsorbent was slightly enhanced in the presence of Na+, Ca2+ and Cl. In general, the adsorption processes at the solid/liquid interface could be affected by the increased ionic strength as a result of the salting out and the squeezing out effects [41, 42]. The salting out effect was previously found to promote the adsorption of 17β-estradiol onto magnetic biochars at a concentration of NaCl below 0.01 mol L−1, but it was subsequently neutralized by the squeezing out effect at high NaCl concentration [31]. Thus, the enhanced adsorption capacity of the AMBC towards RhB in the salts solutions might be caused by the salting out effect. It should be noted that the adsorption capacity of the AMBC in NaCl solutions was always higher than that in CaCl2 solutions at the same ionic strength. This might be attributed to the relative high salt concentration when the ionic strength was adjusted by NaCl. These results ascertained that the cation and anion in the solutions concurrently dominated the adsorption performance of the AMBC.

3.5. Stability and Regeneration of the AMBC

In this study, a 50% of methanol solution was used for desorption of RhB from the AMBC on the basis of large dissolution of RhB in the organic solvent. The adsorption–desorption cycles demonstrated that the used AMBC could be easily regenerated by the methanol solution, without significant loss in the adsorption capacity after 3 cycles in pure water (Fig. 5). However, the removal efficiency of RhB from the simulated wastewater decreased to 71.6% after 3 cycles, which is significantly lower than that of RhB in pure water (92.7–98.3%). This might be caused by the complexity of the matrix, i.e., the cations, anions and other organic pollutants co-existed in the solutions may compete the adsorption sites [38]. Nevertheless, the adsorption performance of the AMBC was still considerable for industrial application. Therefore, the synthesized AMBC could be used as an alternative for removal of organic dyes from wastewaters.

3.6. Mechanisms for RhB Adsorption onto the AMBC

The closeness of the RhB adsorption data to Freundlich isotherm indicated multi-layer adsorption onto the heterogeneous surface of the AMBC. The porous structures of the AMBC facilitated the physical adsorption of RhB, which was corroborated by the calculated ΔG value (< 40 kJ mol−1). Meanwhile, the chemical adsorption processes such as H-bonds and electrostatic interactions were also involved in the processes. These mechanisms were demonstrated by the effects of pH and ionic strength on the adsorption of RhB onto the AMBC and the excellent fitness of pseudo-second order kinetics model to the adsorption data.
To further elucidate the mechanisms for RhB adsorption onto the AMBC, FTIR measurements were compared between the pristine and RhB-loaded AMBC (Fig. 6). The slightly increase in the absorption at 3,430–3,450 cm−1 could be assigned to the O-H stretching of hydroxyl groups [43]. The peaks at 1,560, 1,028 and 490 cm−1 were ascribed to C=C, C–O and Fe–O vibrations in the AMBC, respectively. Compared to the AMBC, the AMBC-RhB composite presented two new absorption peaks at 1,720 and 813 cm−1, corresponding to the stretching vibrations of C=O and N–C of the RhB molecule. Therefore, it is reasonable to speculate that the RhB was adsorbed onto the AMBC by H-bonds. Furthermore, these peaks were shifted by the adsorption of RhB, which indicated that π-π stacking was also involved in the adsorption processes. Similar phenomena were also found with 17β-estradiol and polycyclic aromatic hydrocarbons adsorbing onto graphene oxide [44, 45]. It should be noted that the hydrophobic distribution is a universal interaction between organic pollutants and carbon materials [20, 45], but it might be a less important contributor for RhB (logKOW = 2.38) adsorption onto the AMBC.

4. Conclusions

A novel magnetic biochar (AMBC) was successfully synthesized from NaOH-activated rice straws via a simultaneous carbonization and magnetization method. The magnetization process made the AMBC superior separation nature and adsorption rate, and the alkaline activation promoted the specific surface area and oxygen-containing functions for the adsorbent. These characteristics collectively contributed to the favorable adsorption performance of the AMBC towards RhB. Briefly, the adsorption kinetics could be well described by the pseudo-second order kinetics model, and the adsorption isotherms obeyed the Freundlich model.
Thermodynamic parameters indicated the adsorption of RhB onto the AMBC was spontaneous with a maximum adsorption about 53.66 mg g−1. Although the adsorption performance of the AMBC was strongly affected by the hydro-chemical conditions such as pH, ionic strength and other soluble substances, it could be applied to remove organic dyes at least for RhB from wastewaters through H-bonds, electrostatic attraction and π-π stacking. In short, the synthesized AMBC had the advantageous features of low cost, easy synthetization and separation, and considerable adsorption capacity, thus it would be an alternative for water pollution remediation.

Supplementary Information

Acknowledgments

This work was financially supported by the National Natural Science Foundation of China (41807379), the Applied Basic Research Foundation of Science and Technology Department of Sichuan Province (2019YJ0340), the Fundamental Research Foundation of China West Normal University (18B022,17E053), the Meritocracy Research Foundation of China West Normal University (17YC143), the National Training Programs of Innovation and Entrepreneurship for Undergraduates (201810638013), and the the Program for Team Scientific Research and Innovation of China West Normal University (CXTD2018-13, CXTD2017-2).

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Fig. 1
(a), (b) The SEM images, (c) Nitrogen adsorption-desorption isotherm, (d) Dynamic light scattering spectra and (e) Energy dispersive pattern of the AMBC.
/upload/thumbnails/eer-2019-232f1.gif
Fig. 2
Adsorption kinetics and (a) Intra-particle diffusion model (b) for RhB by the AMBC. Experimental conditions were controlled as CAMBC = 1.0 mg mL−1, CRhB = 50.0 mg L−1, pH = 6.5 and temperature = 25°C.
/upload/thumbnails/eer-2019-232f2.gif
Fig. 3
Adsorption isotherms for RhB by the AMBC at 10°C, 25°C and 40°C. The CAMBC = 1.0 mg mL−1, CRhB=50.0 mg L−1, pH = 6.5 and equilibrium time = 60 min.
/upload/thumbnails/eer-2019-232f3.gif
Fig. 4
Effects of pH and (a) Ionic strength (b) on the adsorption of RhB by the AMBC. CRhB = 50 mg L−1, CAMBC = 1.0 mg mL−1, pH = 6.5, T = 25°C, t = 60 min.
/upload/thumbnails/eer-2019-232f4.gif
Fig. 5
Evaluating the reusability and stability of the AMBC in pure water and simulated wastewater.
/upload/thumbnails/eer-2019-232f5.gif
Fig. 6
FTIR spectra for the AMBC and AMBC-RhB composite.
/upload/thumbnails/eer-2019-232f6.gif
Table 1
Freundlich and Langmuir Isotherms Parameters for the Adsorption of RhB onto the AMBC
Models Temperature (°C)

Parameters 10 25 40
Freundlich Model KF ((mg g−1)·(L mg−1)n) 12.56 16.28 17.68
1/n 0.301 0.296 0.302
Adjusted R2 0.991 0.992 0.981
Langmuir Model Qm (mg g−1) 53.78 66.45 73.47
KL (L mg−1) 0.102 0.125 0.125
Adjusted R2 0.893 0.938 0.910
Table 2
Thermodynamic Parameters for the Adsorption of RhB onto the AMBC
Temperature (°C) ΔG0 (kJ mol−1) ΔH0 (kJ mol−1) ΔS0 (kJ mol−1 K−1)
10 −8.78
25 −9.93 8.32 0.06
40 −10.60
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