The Investigation of Optimizing Leaching Efficiency of Al in Secondary Aluminum Dross via Pretreatment Operations

Abstract

Secondary aluminum dross (SAD) is an inevitable by-product from the secondary aluminum industry and has caused serious environmental issues. In this study, the effect of pretreatment operations on the subsequent acid leaching operation was studied by process mineralogy, a series of leaching experiments, XRD, and SEM. Leaching results showed that the leaching efficiency of Al in direct acid leaching was only 22.99%. Process mineralogy showed the complex intertexture and continuous network structure in the SAD. Pretreatment operations were extremely efficient in destroying the structure by physical and chemical interaction. Interestingly, by adding the grinding and water leaching operations, the leaching efficiency of total aluminum in the SAD reached approximately 28.70%. XRD results showed that nearly all metallic Al, AlN, and partial Al₂O₃ were leached by grinding–water leaching–acid leaching. The scanning electron micrographs showed that the residue particles mainly included some insoluble components and had a smooth surface.

1. Introduction

Secondary aluminum dross (SAD), which forms during the aluminum scrap/dross melting processes, is an inevitable by-product from the secondary aluminum industry [1,2]. Metal aluminum can be recycled almost completely without loss of quality from the aluminum scrap/dross, and the amount of this scrap has been increasing rapidly. The production of secondary aluminum not only saves 95% of the energy but also avoids approximately 95% of the emissions of noxious gas compared with the primary aluminum production from bauxite [2,3,4]. Thus, the secondary aluminum industry has been booming in the past few years.

With the prosperity of the secondary aluminum industry, more than one million tons of SAD are produced every year worldwide [5]. The SAD typically contains aluminum (Al) metal, aluminum oxide (Al₂O₃), aluminum nitride (AlN), halite, sylvite, and other contaminants, and these compounds are harmful to the environment and difficult to recover. The current treatment of the SAD cannot balance the relationship between economy and the environment. Approximately 95% of the SAD has been stacked and landfilled [6,7]. The leachability of the landfilled SAD normally leads to the leaching of toxic metal ions into ground water, and the high reactivity of the SAD with water can result in the formation of toxic, explosive, and poisonous odorous gases, such as NH₃, CH₄, PH₃, H₂, and H₂S [8,9,10]. The toxic metal ions and gaseous emissions from the landfilled SAD is a great environmental concern [8,9,10,11]. Therefore, finding a feasible process for treating SAD is imperative.

The chemical and mineral compositions of SAD in different regions vary greatly because of the diversity of the scrap feed, which is a complex combination of all types of aluminum scraps collected [12,13]. Given the complex compounds and lower Al metal content of the SAD, the hydrometallurgical process is preferred than the pyrometallurgical method in treating the SAD [14]. The former process is sensitive to some impurities in the SAD, necessitating pretreatment before acid/alkaline leaching. The traditional operations in pretreating SAD consist of ball grinding and water leaching. Nevertheless, the previous researchers just used ball milling and water leaching to recover the Al metal and dissolve the salt [15,16]. The researchers neither studied the comprehensive influences of ball milling and water leaching on the subsequent acid/alkaline leaching operation, nor analyzed the mechanism of the operations.

Ball milling plays an important role in recovering Al metal from the SAD. Given the higher ductility and viscosity of the Al metal compared with the other components in the SAD, the Al metal will become increasingly bigger, while the other components will become smaller during the ball-milling operation [17]. Türk et al. [18] studied the effect of particle size on the efficiency of extracting Al. The results showed that ball milling could increase the mechanical activation of the aluminum dross. David et al. [19] investigated the influence of high-speed ball milling on the superficial area of the Al particle in aluminum dross. The results showed that ball milling could not only decrease the particle size and increase the surface area of the aluminum dross but also produce a disordered structure by the agglomeration of microparticles. Thus, ball milling contributed to a reduced reaction temperature and higher chemical reactivity. Moreover, the existence of the hydroxide or oxide protective film on the Al particle surface could be destroyed by ball milling. Nhi et al. [20] found that the milling speed had a great influence on the leaching behavior of silica and the oxides of Ca, Fe, Mg, and Ti in the aluminum dross.

Water leaching is indispensable for high-pressure leaching, because soluble salts have a great effect on the leaching of Al, and some compounds in the SAD can be decomposed by reacting with water to emit explosive gases during digestion [21]. Bruckard et al. [21] determined the feasibility of extracting soluble salts and decomposing aluminum nitrides and carbides in the SAD by water leaching. The results showed that 86–89% of chloride, 54–58% of sodium, and 37–43% of potassium were dissolved during water leaching at 25 °C, whereas only small amounts of the other elements were extracted during the process. Tsakiridis et al. [22] proved that 80% of sodium and 85% of potassium was removed during water leaching at 90 °C, and the yield of black dross was only 89% after water leaching.

The aforementioned studies on ball milling and water leaching have mainly focused on the impact of the operation itself to the SAD and ignored the impact on subsequent acid/alkaline leaching operations. In this paper, the study started from the mineralogical analysis of the SAD, and the results were used to select the appropriate pretreatment operations. A series of comparation experiments were conducted to verify the effect of the pretreatment operations. In addition, the role of pretreatment operations in the leaching of the SAD was investigated through XRD and SEM.

2. Materials and Methods

2.1. Materials

2.1.1. SAD

The SAD sample was supplied by an aluminum company located in Kunming, Yunnan Province, China. The SAD was deep gray in color and smelled pungent, because ammonia is released when the SAD reacts with water in a humid environment. According to the results of the chemical and phase analysis shown in Figures S1 and S2, which were also reported in previous studies [23,24], Al and O compose 77.44% (wt) of the total elements, which mainly exist in the Al phase, alumina (including α-alumina, β-alumina, and γ-alumina), NaAl₁₁O₁₇, and MgAl₂O₄. In addition, Na, K, and Cl compose 14.23%, which are in the salt phase, such as NaCl and KCl. After repeating the leaching operations with the alkaline solution, the total quantity of AlN in the SAD is 14.38%. Thus, the calculated Al element in AlN accounts for 19.35% of the total Al element in the SAD. The SAD contains a small quantity of the impurity elements (e.g., F, Mg, Si, Fe, Ga, Ti, and V).

The results in the analysis of the grain size and metal Al of the SAD are listed in

Table 1. Grain-size and metal aluminum analysis of the secondary aluminum dross (SAD).

Grain-Size (mm)	Yield (%)	Aluminum Grade (%)	Aluminum Distribution (%)
0.25–0.45	6.65	15.26	26.63
0.15−0.25	21.50	5.72	35.18
0.10−0.15	29.71	2.23	18.95
0.076−0.10	24.05	1.81	12.45
0−0.076	18.08	1.31	6.78
Initial SAD	100.00	3.58	100.00

. The Al grade of the initial SAD is 3.58%. The yield of each size fraction is evenly distributed, but the grade of Al varies greatly. The smaller the particle size is, the lower the grade will be. The metal Al grade of (0.25−0.45 mm) size fraction reaches up to 15.26%. However, the grade of the particle size fraction below 0.076 mm is only 1.31%. Thus, the metal Al is mainly distributed with a coarse grain size.

2.1.2. Chemical Reagents

Hydrochloric acid (HCl, 37%), ammonia (25%), and boracic acid (99% purity) were purchased from Hunan Huihong Reagent Co., Ltd. (Changsha, China). All chemicals were used without any additional purification. Deionized water was used at all stages of the experiment unless otherwise stated.

2.2. Methods

2.2.1. Grinding operation

A conical ball mill of XMQ-Φ240 × 90 (Wuhan Prospecting Machinery Factory, Wuhan, China) with a rotational speed of up to 96 rpm was employed for the grinding operation. The grinding operation was performed as follows. SAD (500 g) and deionized water (300 mL) were mixed to form a slurry with 60% concentration. The mixture was added into the ball mill with 7.6 kg of iron balls and then milled for 2.5, 5, 7.5, 10, and 20 min at 96 rpm. Then, the slurry in the ball was rinsed using 920 mL of the deionized water, which needed to be strictly controlled so that the liquid-solid ratio of the subsequent leaching operation was 50 mL/20 g.

2.2.2. Leaching Operation

The schematic of the leaching device is presented in Figure S2, which was previously reported [23,24]. Each experiment for the leaching of the SAD was performed in a 250 mL conical flask, which was placed in an oil bath and heated at a fixed test temperature. For each leaching operation, 50 mL of the corresponding leaching solution was first added to the conical flask, and then the Electro-Thermostatic water bath was turned on to heat the solution to the required temperature before 20 g of the solid sample was added. Then, the slurry was agitated at different temperatures and time. Finally, the slurry was filtered with a Buchner funnel to collect the pregnant liquor to measure the amount of ammonia nitrogen and the concentration of Al. The leaching residues were dried and weighed.

2.3. Detection and Analysis Methods

The total aluminum concentration in the leaching solution was determined by inductively coupled plasma optical emission spectrometer (ICAP7400 Radial, Thermo Fisher Scientific company, Waltham, MA, USA) to calculate the leaching efficiency of total aluminum. The detailed analysis conditions include wavelength range: 166−847 nm; optical system: constant temperature drive type; light chamber temperature: precise constant temperature 38 ℃ ± 0.1 ℃; optical resolution: ≤0.007 nm at 200 nm, 0.014 nm at 400 nm, 0.021 nm at 600 nm; plasma observation method: vertical observation of vertical flame. Nessler’s Reagent Spectrophotometry (HJ535-2009) was used to determine the ammonia nitrogen in the leaching solution. The specific test method and principle were introduced in our previous paper [23].

After the initial sample was received from Kunming, Yunnan Province, China, the samples were first mixed several times to make the components uniform. Then, the imbedded characteristics of the initial SAD were examined by using a polarized light microscope (Leica DMLA, Wetzlar, Germany), and the grain size was analyzed by using a series of sieves with different apertures. After the initial SAD was ground with an agate mortar to make particles with size ≤44 μm, the elemental and mineralogical analyses were performed by X-ray fluorescence (XRF, Axiosm AX, Panalytical. B. V, Almelo, The Netherlands) and X-ray diffraction (XRD, X-Pert³ Powder, Panalytical. B. V, Almelo, The Netherlands), respectively. Finally, the morphology of the SAD was explored by scanning electron microscopy (SEM; Phenom ProX scanning electron microscope). To explore the variation in the leaching residues compared with the initial SAD, all aforementioned analyses, except the measurements from the polarized light microscope and XRF, were also used to determine the characteristic of the leaching residues.

3. Results and Discussion

3.1. Direct Acid Leaching Process

Metal Al and some Al compounds in the SAD are amphoteric, which can be dissolved in either acidic or alkaline solutions. The acid solution has a strong reaction ability and can leach various metal oxides, such as magnesium oxide, ferric oxide, and calcium oxide from the SAD. Thus, the acid leaching residue almost does not contain metal impurities. In contrast, the alkaline solution can just leach SiO₂ from SAD, except Al compounds, and a relatively pure leaching solution can be obtained. HCl, which is generated as a by-product in many chemical industries [25,26], is a versatile acid and readily available. In addition, to obtain a relatively pure leaching residue for refractory and building materials, HCl has been selected as the leaching agent of the SAD. The reaction in the leaching solution is as follows:

Al(s) + 3HCl(aq)→AlCl₃(aq) + 1.5H₂(g)

(1)

AlN(s) + 4HCl(aq)→AlCl₃(aq) + NH₄Cl(aq)

(2)

Al₂O₃(s) + 6HCl(aq)→2AlCl₃(aq) + 3H₂O

(3)

Fe₂O₃(s) + 6HCl(aq)→2FeCl₃(aq) + 3H₂O

(4)

CaO(s) + 2HCl(aq)→CaCl₂(aq) + H₂O

(5)

MgO(s) + 2HCl(aq)→MgCl₂(aq) + H₂O

(6)

In the HCl solution, corundum and magnesia-alumina spinel are sufficiently stable and insoluble. Thus, the efficiency of leaching the total Al is the sum of the efficiencies in extracting Al, AlN, and activated-Al₂O₃. To determine the contribution of each Al component to the leaching rate of the total Al, the decomposition rate of AlN obtained by the analysis of ammonia nitrogen in the leachate should be known when the efficiency in leaching Al and activated-Al₂O₃ is difficult to detect.

Prior to the optimization of the leaching temperature and time, a series of experiments were conducted to determine the optimal acid concentration (6 mol/L), liquid-to-solid ratio (L/S) (50 mL/20 g), and stirring speed (300 rpm). The results are shown in Figures S3–S5. The optimal conditions were used in all subsequent tests. Figure 1 exhibits the variation of the decomposition of AlN at different temperatures. As shown in Figure 1, as the leaching time progresses, the decomposition rate of AlN increases rapidly in the first 60 min. When leaching time is higher than 60 min, the decomposition rates of AlN at 298.15 K and 348.15 K are basically unchanged, demonstrating that the leaching process has reached equilibrium. However, at 323.15 K, the curve keeps an almost average rate of increase over time. According to a previous study [24], the high activation energy (40.93 kJ/mol) of the reaction between AlN and HCl is the main reason for the overall trend of the AlN decomposition curve. In addition, the highest decomposition ratio of AlN is approximately 42.5% in the HCl solution at 348.15 K.

Figure 2 presents the effects of temperature on the efficiency of leaching total Al at different times. With the increase in temperature and extension of leaching time, the efficiency of leaching the total Al shows a similar trend with the decomposition rate of AlN. This result indicates that the extraction of AlN accounts for a large proportion of the leaching efficiency of the total Al. The higher the temperature is, the higher the efficiency of leaching the total Al will be. The results indicate that when the leaching temperature is increased from 298.15 K to 348.15 K, the efficiency of leaching the total Al rises from 14% to 22.99%. To determine the reason for the low leaching efficiency, the inlay structure and the leaching mechanism of all components in the SAD need to be explored. Thus, the process mineralogy of the SAD was investigated.

3.2. Investigation of the Process Mineralogy of the SAD

According to the XRD pattern of the SAD in Figure S1 [24], the SAD mainly constitutes seven phases, namely, metallic Al, NaCl, AlN, corundum (α-alumina), β-alumina (NaAl₁₁O₁₇), magnesia-alumina spinel (MgAl₂O₄), and silicon dioxide (SiO₂). To explore the complex inlay structure of these phases in the SAD, the process mineralogy of the SAD, which is usually used to analyze the inlay structure of ore in nature before the beneficiation process, was performed. The specific inlay structure of SAD is shown in Figure 3.

The microstructures of the SAD observed using an ore microscope are presented in Figure 3. Figure 3a shows that the metal Al in the SAD, with size ranging from 20 μm to 200 μm, is mainly round and covered with inhomogeneous oxide layers. The layers consist of fine alumina particles and are 2–20 μm thick (Figure 3b). The alumina mainly exists as fine particles with the size range of 2–200 μm (Figure 3e) and a small amount as flakes (Figure 3f). The complex interwoven structure between the Al metal and alumina is shown in Figure 3d. The alumina layer covers the Al metal, which contains alumina particles. The encapsulated metallic Al cannot be in contact with the acid leachate to be extracted, unless the superficial alumina is destroyed or dissolved in the leachate. However, the superficial alumina (α-alumina) is primarily stable and insoluble in the acid solution. The best way to release the metallic Al is to destroy the superficial layer by the external mechanical forces from ball milling.

Figure 3c presents that part of the metallic Al, which is generally smaller than 5 μm, agglomerates or bonds with fine particles, such as Al₂O₃, AlN, and aluminate, to form a continuous network structure with particle size ranging from 30 μm to 200 μm. In a previous study [23,24], the degree of decomposition of AlN in the aqueous solution is better than that in HCl. This result indicates that the AlN in a continuous network structure can decompose more completely by water leaching. The Al(OH)₃ formed by the hydrolysis of AlN is very easy to dissolve in HCl solution, which can produce small bores to destroy the structure and release more soluble Al components. Therefore, the efficiency of leaching the total Al can be optimized by the water leaching operation.

The SAD is formed during the Al scrap/dross melting processes. Thus, the seven phases of the SAD are tightly bound in a very complex structure, which can be confirmed by the analysis of process mineralogy. The interwoven and continuous network structures severely hinder the contact between the soluble Al components and the leachate and significantly affect the efficiency of leaching the total Al. To destroy the compact structure to increase the superficial area and release the soluble aluminum components [26], pretreatment is extremely essential. Moreover, the mechanical activation of SAD is greatly improved by ball milling, which increases the rate of leaching the SAD [18]. Water leaching can remove the majority of most soluble salts to enhance the efficiency of leaching the total Al and decompose harmful materials that can react with water to emit some pungent explosive gas [21].

3.3. Effects of the Pretreatment Operation on Acid Leaching

3.3.1. Effect of Ball-Grinding Operation

Mechanical ball milling refers to a process that uses mechanical forces, such as grinding, impact, and shearing, to promote the physical and chemical changes in substances. Changes in the SAD caused by ball milling includes the reduction of particle size, more cracks, increase in the superficial area, and removal of pellumina on the metallic Al surface. Figure 4 indicates the effect of grinding time on the particle size of the SAD. Figure 4a shows that the particle size of the SAD decreases sharply at the beginning, the proportion of the particle size fraction below 76 μm in the SAD increases from 18.08% to 80% after grinding for 2.5 min. Thereafter, the particle size decreases steadily at a slower speed, and the particle size fraction below 76 μm fraction accounts for 96% after 20 min of grinding. As the particle size decreases, the complex inlay structure of SAD is destroyed, and the mechanical activation of the SAD system is promoted [18].

Considering simultaneously the loss of electric energy and the grinding effect, 2.5 min was selected as the optimal milling time to conduct the subsequent experiments, and 348.15 K was chosen as the optimal leaching temperature. Figure 4b presents the effect of grinding on the decomposition rate of AlN at 348.15 K in the HCl solution. As shown in Figure 4b, regardless of whether a ball milling operation is performed, the variations of the curves are similar. The decomposition rate of AlN increases sharply in the first 120 min and continues to ascend slightly thereafter. At 373.15 K, the final decomposition rate of AlN reaches 46% after grinding, which is only 4% higher than that without the grinding operation. The decomposition of AlN is suppressed to some extent due to the nature of HCl. Thus, the grinding operation cannot improve obviously the decomposition rate of AlN. However, the reaction rate significantly increases with the improvement of the mechanical activation of the SAD system.

The effect of grinding on the efficiency of leaching the total Al at 348.15 K in the HCl solution is shown in Figure 4c. The grinding operation dramatically improves the efficiency of leaching the total Al, which increases initially and then remains at equilibrium in the two curves. By comparing the two final equilibrium values, the efficiency of leaching the total Al after grinding is 5.43% higher than that without grinding. The increase in this efficiency is markedly higher than the decomposition of AlN, because the Al element in AlN only accounts for 19.35% of the total Al element in the SAD. Thus, the grinding operation mainly improves the efficiency of leaching metallic Al and alumina in the SAD by exposing more metallic Al particles and increasing the mechanical activation of the SAD system.

3.3.2. Effect of Water Leaching Operation

Water leaching is the conventional pretreatment of the SAD to remove the Na and K salts. Bruckard et al. [21] proved that soluble salts had a great effect on the leaching of the total Al in the SAD. Thus, to some extent, water leaching can improve the efficiency of leaching the total Al. However, the feasibility of determining the efficiency of leaching the total Al on the basis of a noncompact structure created by the reaction between water and AlN is rarely studied. The AlN in the SAD can be hydrolyzed in water leaching and turn to Al(OH)₃ and NH₃. Then, NH₃ dissolves in water, increasing the solution pH, which enhances the reactivity of Al, Al₂O₃, and AlN. The reactions in the water leaching operation are as follows:

AlN(s) + 4H₂O → Al(OH)₃(s) + NH₃·H₂O(aq)

(7)

2Al(s) + 6H₂O → 2Al(OH)₃(s) + 3H₂(g)

(8)

NaCl → Na⁺ + Cl⁻

(9)

KCl → K⁺ + Cl⁻

(10)

In Figure S6 [23], the hydrolysis of AlN in the SAD results in the 59% and 41% decomposition ratio of AlN at 348.15 K and 323.15 K, respectively. Approximately 67% of AlN is decomposed after reacting with water for 240 min at 375.15 K, which is the highest decomposition rate of AlN. By comparing the optimal decomposition rates of AlN in water and HCl, AlN reacts more easily with water than with HCl [24]. Moreover, the product of hydrolysis is more soluble than AlN in HCl. Thus, the decomposition rate of AlN is promoted by water leaching.

Figure S7 presents the effect of the water leaching temperature on the efficiency of leaching the total Al at different times. The efficiency of leaching the total Al in the SAD is almost maintained at zero in the different temperatures during the water leaching process. The Al element in AlN and Al metal in the SAD are transformed into Al(OH)₃, which is insoluble in water [23]. The newly formed Al(OH)₃ dissolves more easily than AlN in subsequent acid leaching operations, which provides favorable conditions for the leaching of Al in the SAD [24].

Figure 5 exhibits the effect of different operations on the efficiency of leaching the total Al at 348.15 K at different leaching times. The efficiency with water leaching is markedly higher than that in leaching with acid only in the first 60 min, and the gap gradually decreases thereafter. When the two curves in Figure 5 reach equilibrium, the efficiencies of leaching the total Al are 22.99% and 24.34% in the two different operations, respectively. Water leaching can significantly increase the reaction rate of Al leaching based on the noncompact structure created by the reaction between water and AlN. However, the leaching efficiency of total Al only increases slightly because of the large particle of the SAD and the low mechanical activation of the SAD system.

3.3.3. Comparison of Different Leaching Operations

The results of direct acid leaching, water leaching–acid leaching, ball milling–acid leaching and ball milling–water leaching–acid leaching are shown in Figure 6. Under the leaching process using HCl only, the extraction efficiency of Al increases rapidly in the first 60 min and then slowly to approximately 22.99% until 360 min. When the SAD was ground before HCl leaching, the trend of the extraction efficiency of the Al of the SAD is in accordance with that with the acid-only leaching. However, the final leaching efficiency reaches 28.42%, which is 5.43% higher than that of the direct acid leaching. This result indicates that ball milling effectively destroys the complex inlay structure and the pellumina on the surface of metallic metal and simultaneously increases the mechanical activation of the SAD system. By adding the water leaching pretreatment process, the extraction efficiency of Al reaches the highest value of 24.34% in 60 min and then remains constant. Although the reaction between water and AlN creates a noncompact structure to increase the extraction efficiency of Al, the particle size of the SAD remains large, and the mechanical activation of the SAD system is low. Thus, water leaching improves the extraction efficiency of Al by only 1.35%. When the two pretreatment operations are added simultaneously, the extraction efficiency of the total Al peaks at 28.70% in the acid leaching within a mere 10 min. To reach the similar efficiency of extracting the total Al, 240 min is imperative during ball milling–acid leaching. The lower extraction efficiency of Al mainly shows the high proportion of the insoluble Al compounds, including corundum and magnesia-alumina spinel in the SAD. Hence, adding water leaching and ball-milling can not only increase the extraction efficiency of Al but also significantly accelerate the reaction rate of Al in the acid leaching procedure.

3.4. Analysis of the Evolution of Phases and Morphology

The XRD patterns of the SAD under different treatments are shown in Figure 7. As shown in Figure 7a, the ground SAD has similar mineralogical phases compared with the initial SAD, presenting almost the same peak except the attenuation of the NaCl peak, which is due to the wet grinding operation. After the water leaching operation is added, some changes, including the disappearance of the salt phase, the attenuation of the diffraction intensity of the AlN peaks, and the appearance of the new Al(OH)₃ phase, can be observed in Figure 7b. The majority of the AlN in the SAD turns to Al(OH)₃ by the grinding-water leaching process. Comparison of Figure 7b,c shows that the diffraction intensities of the peaks of corundum (α-Al₂O₃), diaoyudaoite (β-Al₂O₃), spinel (MgAl₂O₄), and quartz (SiO₂) increase, and the phases of Al and Al(OH)₃ disappear with time. Al and Al(OH)₃, which are formed in the reaction between AlN and water, are decomposed, and the other components are insoluble in HCl. The diffraction intensity of the Al₂O₃ peaks remains constant, which can indicate that Al₂O₃ just slightly dissolves in HCl. As a result, nearly all metal Al, AlN, and partial Al₂O₃ are leached by the grinding–water leaching–acid leaching process.

Figure 8 shows the microstructures of the SAD after the different treatments. As shown in Figure 8a, the initial SAD has an irregular shape and rugged surface and is covered by many salt granules. Moreover, several components in the SAD are closely linked together, and only partial metallic Al in the SAD is exposed. After grinding, Figure 8b clearly shows the fracture surface of the Al metal released from the Al oxide layers, and the salt granule decreases. These phenomena indicate that the wrapped metallic Al in the initial SAD is released, and the pellumina is destroyed by ball milling. After the grinding–water leaching operation, the round and nonangular SAD with different particle sizes and some tiny Al(OH)₃ particles can be seen in Figure 8c. This result suggests that the salt components on the SAD surface are dissolved completely, and AlN is decomposed and transformed into the Al(OH)₃ phase. From Figure 8d, the residual dregs, which mainly include some insoluble components, such as corundum and magnesia-alumina spinel in the HCl solution, show a smooth surface and are smaller than the initial SAD. This phenomenon is verified from the XRD results.

4. Conclusions

In this study, grinding and water leaching are potential pretreatment operations to increase the leaching efficiency of the non-refractory Al components such as metallic Al and AlN in the SAD in the subsequent acid leaching operation. The leaching efficiency of Al was only 22.99% under the direct acid leaching process. Thus, the process mineralogy of SAD was investigated to observe the complex intertexture and continuous network structure in the SAD. Adding ball milling or water leaching operation resulted in leaching efficiencies of 28.42% and 24.34%, respectively. Ball milling mainly exposed more metallic Al and alumina particles and increased the mechanical activation of the SAD system. Water leaching led to the noncompact structure created by the reaction between water and AlN to slightly improve the efficiency of leaching Al. The XRD and SEM results verified the chemical and phase analyses. As a result, pretreatment operations can increase approximately 5.71% of the Al leaching efficiency from the SAD in the subsequent acid leaching operation.