Microbial Bioleaching of Critical Metals from Spent Lithium-Ion Batteries: A Biohydrometallurgical Approach

Abstract

Biohydrometallurgical processing of spent lithium-ion batteries offers a low-impact route for critical metal recovery compared with conventional hydrometallurgy. In this work, the iron-oxidizing bacterium Acidithiobacillus ferrooxidans was evaluated for the bioleaching of cobalt (Co), nickel (Ni), lithium (Li) and copper (Cu) from pyrolyzed industrial black mass derived primarily from LiCoO₂-based batteries, containing both LiCoO₂ and LiNiO₂ layered oxide phases. Batch experiments were conducted in 9K medium at 30 °C, varying pulp density (1%–2%, w/v), inoculum volume (10–20 mL in 200 mL medium) and initial pH (with and without adjustment). At 1% pulp density and 10% v/v inoculum, metal recoveries after 6–7 days reached about 64%–70% Co, 57%–72% Ni, 52%–60% Li and 81%–100% Cu, with most dissolution occurring in the first 6 days. Higher inoculum loads without initial pH adjustment increased Li recovery up to 79%, but did not further improve Co and Cu, indicating a trade-off between microbial activity, metal toxicity and ferric iron availability. The temporal evolution of pH and metal dissolution is consistent with indirect redoxolysis by biogenic Fe³⁺ and sulfuric acid generated during ferrous iron and elemental sulfur oxidation. Overall, the results confirm the feasibility of A. ferrooxidans-assisted bioleaching as a green option for Co, Ni, Li and Cu recovery from spent LiCoO₂ batteries and provide operating windows for subsequent process optimization and scale-up.

1. Introduction

Waste electrical and electronic equipment (WEEE) is one of the fastest-growing waste streams worldwide, driven largely by the rapid expansion of portable electronics and electric mobility [1,2]. Spent lithium-ion batteries (LIBs) form a critical fraction of WEEE, as they contain significant amounts of valuable and critical raw materials such as cobalt (Co), lithium (Li), and nickel (Ni), which are indispensable for modern energy technologies and are officially recognized as critical by the EU and other international bodies [3,4,5].

Conventional recycling of spent LIBs is currently dominated by pyrometallurgical and hydrometallurgical routes, as well as emerging electrochemical processes [6,7,8,9,10]. Pyrometallurgy typically employs high-temperature smelting to recover metallic alloys but is energy intensive and often associated with substantial gaseous emissions and complex off-gas treatment [11,12,13]. Hydrometallurgical processes based on strong mineral acids (e.g., H₂SO₄, HCl, HNO₃, H₃PO₄), reducing agents, and multi-step separation schemes (precipitation, solvent extraction, ion exchange) can achieve high recoveries and high purity products, but they require significant chemical inputs and generate secondary effluents that must be carefully managed [14,15,16,17]. Recently, electrochemical recycling has attracted attention as a potentially cleaner, electricity-driven alternative; however, it is still at an early development stage and often needs precise control and relatively pure feed streams [18,19].

At the same time, most conventional routes are optimized for specific battery chemistries and may not be easily adaptable to the increasingly diverse LIB compositions entering the waste stream, particularly those containing complex cathode materials such as lithium cobalt oxide (LCO) [3,7]. For LCO-based batteries, cobalt remains the primary economic driver for recycling, but the simultaneous recovery of Li and Ni is increasingly important to ensure resource efficiency and to support circular economy strategies for critical raw materials (CRMs) [4,6].

Bio-hydrometallurgy has therefore emerged as a promising ‘green’ alternative or complement to existing recycling practices, enabling metal solubilization under mild operating conditions through the metabolic generation of acids and oxidants [20,21,22]. Bioleaching, the most widely applied bio-hydrometallurgical approach, has been used extensively in mining and is now gaining traction for the treatment of industrial residues and the black mass of spent LIBs [1,20,23,24]. The efficiency of microbial metal solubilization depends strongly on the characteristics of the feed material and on the composition of the cultivation medium [25,26]. Different microbial groups contribute distinct lixiviants: acidophilic sulfur- and iron-oxidizing bacteria such as Acidithiobacillus ferrooxidans and Acidithiobasillus thiooxidans generate ferric iron and sulfuric acid, which are potent oxidants for transition-metal-bearing phases [27,28], while filamentous fungi such as Aspergillus niger and Penicillium chrysogenum produce organic acids that promote the complexation and mobilization of Co, Ni, Li and Cu from secondary resources [22,29,30].

In addition to microbial type, the chemical composition of the cathode material strongly influences bioleaching behavior, since different battery chemistries exhibit distinct crystal structures, redox properties and metal dissolution mechanisms [20,26,31]. Layered oxide cathodes such as LCO and LiNixMnyCozO₂ (NMC) are generally amenable to indirect redoxolysis mediated by biogenic Fe³⁺ generated by iron-oxidizing bacteria, which promotes dissolution of Co and Ni under acidic conditions [20,23,27]. In contrast, olivine-structured LiFePO₄ (LFP) cathodes exhibit stronger phosphate bonding and structural stability, which can limit ferric-iron-driven redoxolysis and often require enhanced acidolysis or consortium-based approaches for efficient lithium recovery [25,28]. Moreover, the relative abundance of transition metals influences both the economic incentive for recycling and the potential inhibitory effects of dissolved metals on microbial activity, particularly at elevated pulp densities [26]. Consequently, battery chemistry plays a decisive role in determining metal recovery efficiency, microbial stability and overall process optimization strategy [26,31].

Recent comprehensive evaluations of microbial LIB bioleaching systems indicate that lithium dissolution is generally faster and more complete than cobalt dissolution, often exceeding 90% under optimized laboratory conditions, whereas Co recovery is more sensitive to redox potential, ferric ion availability, and pulp density [26]. Acidophilic chemolithoautotrophic bacteria promote metal solubilization primarily through acidolysis and redoxolysis mechanisms driven by biologically generated ferric iron and sulfuric acid, while heterotrophic fungi operate mainly via complexolysis mediated by organic acids such as citric, oxalic and gluconic acids [31,32]. These mechanistic differences significantly influence selectivity, kinetics and process robustness when treating complex LCO-derived black mass [26,31].

For spent LCO batteries, acidophilic bacteria are of particular relevance, as they operate effectively at low pH and moderate temperatures, conditions that align with both the stability window of cobalt-rich oxides and the requirements of industrial bioleaching practice [33,34]. A wide range of biocatalysts, media formulations and operational strategies has been explored in the literature, but systematic optimization remains limited, particularly for real industrial black mass, whose composition, microstructure, and impurity profiles differ markedly from synthetic or laboratory-prepared materials [26,35,36]. Parameters such as pulp density, initial pH, temperature, redox potential, inoculum size, and availability of energy sources (Fe²⁺, S⁰) have been identified as key factors controlling bioleaching performance, but their interactions are still not fully understood for complex LIB residues [23,37]. Recent studies emphasize that systematic optimization approaches, including response surface methodology, adaptive culture strategies and thermodynamic modeling, are essential for maximizing metal recovery from real industrial black mass [2,23]. Several studies have reported that increasing pulp density beyond 2%–5% (w/v) can reduce bacterial activity due to elevated dissolved metal concentrations and associated oxidative stress, while higher redox potentials associated with ferric iron generation correlate positively with cobalt dissolution efficiency [38,39]. Optimal performance is generally observed at pH values between 1.5 and 2.5 [31,40]. Moreover, microbial adaptation to elevated metal concentrations and regulation of intracellular reactive oxygen species have been identified as promising strategies to improve bioleaching robustness and scalability [26,31].

From a process-engineering perspective, bioleaching offers several advantages over conventional physicochemical recycling routes [41,42]. Operation near ambient temperature and atmospheric pressure significantly reduces energy consumption compared with pyrometallurgical processes [11,20,43]. The metabolites generated by microbial activity are generally less hazardous and easier to manage than strong mineral acids, thereby lowering the risk of secondary environmental contamination [43,44]. In some cases, bioleaching can also provide partial selectivity toward specific metals or oxidation states, which may reduce downstream purification requirements. However, practical challenges remain, including slow kinetics compared with conventional hydrometallurgy, sensitivity of microbial cultures to toxic shock or contamination, and limitations in reactor scale-up and process control [31,45]. Recent studies have begun to address these limitations. For instance, Alipanah et al. [23] applied design-of-experiments methodologies and thermodynamic modeling to optimize bacterial bioleaching of spent LIBs, demonstrating significant recovery of Li, Co, Ni, and Mn under well-tuned conditions.

Within this context, Acidithiobacillus ferrooxidans is an especially attractive biocatalyst for the bioleaching of LCO-derived black mass [23,27,46]. This acidophilic, chemolithoautotrophic bacterium derives energy from the oxidation of ferrous iron and reduced sulfur compounds, generating ferric iron and sulfuric acid that act as powerful oxidizing and acidifying agents for metal dissolution [23,46,47]. It grows optimally at 20–35 °C and pH 1.5–3.5, conditions that align with efficient LCO dissolution and with the elevated metal loadings typical of industrial black mass. Its ability to grow autotrophically via CO₂ fixation simplifies medium formulation and reduces contamination hazards in long-term operation [27,46,48].

The aim of this study is to systematically evaluate the bioleaching performance of Acidithiobacillus ferrooxidans for the recovery of Co, Li, and Cu from industrially pre-treated, LCO-derived black mass under controlled batch conditions. Unlike many previous studies based on synthetic cathode powders or simplified laboratory systems, this work focuses on real pyrolyzed industrial black mass characterized by heterogeneous composition and impurity profiles. Specifically, the objectives are to: (i) quantify metal recovery efficiencies under varying inoculum volumes and pulp densities; (ii) investigate the influence of both initial and dynamically evolving pH conditions on dissolution kinetics; (iii) correlate microbial growth behavior with acid generation and metal solubilization trends; and (iv) characterize post-leaching residues to confirm selective removal of metal-bearing phases. By defining operational windows that maximize Co dissolution while ensuring significant co-recovery of Ni and Li, this study provides experimentally validated parameters and mechanistic insight to support future optimization and scale-up of biohydrometallurgical treatment routes for industrial LCO-derived black mass.

2. Materials and Methods

2.1. Materials

2.1.1. Industrial LCO-Derived Black Mass

The feed material (black mass) used in this study originated from industrially pre-treated lithium-ion batteries derived primarily from LiCoO₂-based cathode systems. The batteries had undergone industrial pre-treatment, including thermal processing (pyrolysis) and mechanical size reduction. Phase characterization (Section 3.1.3) confirmed that the resulting black mass contains both LiCoO₂ and LiNiO₂ layered oxide phases, indicating a cobalt-dominant mixed cathode composition typical of industrial LCO-derived streams rather than a strictly single-phase LiCoO₂ material. The resulting black mass consists of cathode and anode active materials, current collector fragments, and other electrode components in powder form with heterogeneous particle size distribution. Prior to use in bioleaching experiments, the material was homogenized by gentle mixing and stored in sealed containers at room temperature to avoid moisture uptake and contamination.

The elemental composition of the black mass was determined by acid digestion followed by Atomic Absorption Spectroscopy (AAS) analysis. Approximately 0.2 g of dry black mass was digested in an autoclave bomb using freshly prepared aqua regia (HCl:HNO₃ molar ratio 3:1; 9.6 mL HCl and 2.4 mL HNO₃), at 80 °C for 2 h under continuous stirring at 250 rpm to ensure complete dissolution. After cooling, the digest was filtered through blue-band filter paper, quantitatively transferred to a volumetric flask, and diluted to 25 mL with ultrapure water prior to analysis. Cobalt, nickel, copper, iron, zinc, manganese, and lithium concentrations were quantified, and metal contents (mg/kg) in the black mass were calculated using the dilution factor and the liquid-to-solid ratio employed.

2.1.2. Reagents

All solutions were prepared with ultrapure water (18.2 MΩ·cm) obtained from a Barnstead™ Easypure™ II system (Thermo Scientific, Waltham, MA, USA). Sulfuric acid (≥95% w/w, TraceSELECT, Honeywell Fluka, Seelze, Germany) was used for pH adjustment of media and leachates, as well as for preparation of the 5 M H₂SO₄ stock solutions employed in cultivation and 9K media. Analytical-grade chemicals used for the preparation of the cultivation medium (Medium 882, Leibniz-Institute DSMZ, Braunschweig, Germany) and the iron-rich 9K bioleaching medium included (NH₄)₂SO₄, MgCl₂·6H₂O, KH₂PO₄, CaCl₂·2H₂O, KCl, K₂HPO₄, MgSO₄·7H₂O, Ca(NO₃)₂, FeSO₄·7H₂O, and trace elements (MnCl₂·4H₂O, ZnCl₂, CoCl₂·6H₂O, H₃BO₃, Na₂MoO₄, CuCl₂·2H₂O).

2.1.3. Microorganism

Bioleaching experiments were carried out using the acidophilic, chemolithoautotrophic bacterium Acidithiobacillus ferrooxidans, obtained as an active culture from the Leibniz Institute DSMZ—German Collection of Microorganisms and Cell Cultures (Braunschweig, Germany). This bacterium was selected based on previous studies demonstrating its effectiveness in metal bioleaching and cobalt recovery from secondary resources and spent LIBs, as well as its ability to use ferrous iron as an energy source and to thrive in highly acidic, metal-rich environments.

2.2. Characterization of Black Mass

2.2.1. X-Ray Fluorescence (XRF)

Elemental composition and major metal oxides in the black mass were determined by energy-dispersive X-ray fluorescence (ED-XRF) using an Epsilon 1 spectrometer (Malvern Panalytical Ltd., Malvern, UK) equipped with an Ag-anode X-ray tube operated at 50 kV and 1 mA and a high-resolution silicon drift detector (SDD). Approximately 4 g of black mass were pressed or loaded into sample cups, and spectra were collected for 30 min per sample to ensure adequate counting statistics. Quantification of major oxides such as CuO, Co₃O₄, NiO phases was carried out using the instrument software and appropriate calibration CRMs standards.

2.2.2. X-Ray Diffraction (XRD)

Crystalline phases present in the black mass before and after bioleaching were identified by XRD using a BRUKER D8 ADVANCE diffractometer equipped with Cu-Kα radiation (λ = 1.5418 Å) LYNXEYE 1D position-sensitive detector (Bruker Corp., Karlsruhe, Germany). Measurements were performed at 40 kV and 40 mA over a 2θ range of 10–90°, with a step size of 0.05° and a total scan time of 30 min per sample. Diffraction patterns were evaluated to confirm the presence of LiCoO₂, LiNiO₂, and graphite in the initial black mass, as well as to assess residual phases in the solid residues after bioleaching.

2.2.3. Scanning Electron Microscopy (SEM) and Energy Dispersive Spectroscopy (EDS)

The microstructure and local elemental composition of black mass particles and bioleached residues were examined by SEM using a JEOL JSM-6380LV microscope (JEOL Ltd., Tokyo, Japan) operated at 20 kV, coupled with an INCA X-Sight EDS microanalysis system (Oxford Instruments Abingdon, UK). Samples were dried, mounted on aluminum stubs, and coated with a thin conductive layer (e.g., Au) before imaging. SEM images were recorded at various magnifications to visualize particle morphology, graphite matrix, and metal-rich grains, while point EDS spectra were used to quantify the relative abundances of Co, Ni, Fe, Al, Si, Ca, and other elements in selected particles.

2.3. Cultivation of Acidithiobacillus ferrooxidans

The cultivation protocol recommended by DSMZ for Medium 882 was followed, with minor adaptations. Three stock solutions, designated A, B, and C, were prepared and subsequently combined to obtain the final cultivation medium.

Solution A consisted of 950 mL of ultrapure water containing 132 mg (NH₄)₂SO₄, 53 mg MgCl₂·6H₂O, 27 mg KH₂PO₄, and 147 mg CaCl₂·2H₂O; the pH was adjusted to 2.3 with 5 M H₂SO₄, and the solution was dispensed into conical Erlenmeyer flasks, sealed with hydrophobic cotton and aluminum foil, and sterilized at 121 °C for 20 min. Solution B consisted of 50 mL of 0.1275 M H₂SO₄ (initial pH ≈ 1.2) containing 20 g FeSO₄·7H₂O; it was similarly dispensed, sealed, and autoclaved at 121 °C for 20 min. Solution C, a trace element solution, was prepared by dissolving 76 mg MnCl₂·4H₂O, 68 mg ZnCl₂, 64 mg CoCl₂·6H₂O, 31 mg H₃BO₃, 10 mg Na₂MoO₄, and 67 mg CuCl₂·2H₂O in 1000 mL of distilled water; flasks were sealed and sterilized at 112 °C for 30 min.

The final cultivation medium (1001 mL) was prepared by mixing 950 mL of Solution A with 50 mL of Solution B and adding 1 mL of Solution C, resulting in a solution with pH 2.3. This medium was distributed into five Erlenmeyer flasks (200 mL each) and inoculated with 1 mL of A. ferrooxidans suspension per flask. Flasks were sealed with hydrophobic cotton and aluminum foil and incubated at 30 °C in an orbital shaker-incubator (ES-20, Biosan LLC, Riga, Latvia) at 100–120 rpm for 5 days to allow microbial growth and activation. During incubation, the bacterium developed a biofilm-like layer at the bottom of the flasks, which progressively covered the base by the end of the 5-day period.

2.4. Bioleaching Medium and Experimental Design

An iron-rich 9K medium was used as the leaching medium to provide ferrous iron as the energy source for A. ferrooxidans. The medium was prepared in 1 L of ultrapure water and contained 3 g (NH₄)₂SO₄, 0.1 g KCl, 0.5 g K₂HPO₄, 0.5 g MgSO₄·7H₂O, 0.01 g Ca(NO₃)₂, and 44.7 g FeSO₄·7H₂O. After distribution into Erlenmeyer flasks, the medium was sterilized at 121 °C for 20 min; upon cooling, its natural pH (≈3.5) was adjusted to 2.5 using 0.5 M H₂SO₄ unless stated otherwise. The trace mineral solution was added from a sterile stock solution and was prepared by dissolving the following compounds in a 1.5 g·L⁻¹ nitrilotriacetic acid disodium salt solution (quantities were reported in g·L⁻¹): 1.00 NaCl, 0.50 MnSO₄, 0.10 FeSO₄·7H₂O, 0.10 CoCl₂·6H₂O, 0.10 CaCl₂·2H₂O, 0.13 ZnCl, 0.01 CuSO₄·5H₂O, 0.01 AlK(SO₄)₂·12H₂O, 0.025 Na₂MoO₄·2H₂O and 0.01 H₃BO₃, as described in [21].

Bioleaching experiments were conducted to examine the influence of inoculum volume, pulp density, and initial pH on metal dissolution from LCO-derived black mass. All tests were carried out in 250 mL Erlenmeyer flasks containing 200 mL of leaching suspension and incubated in an orbital shaker at 30 °C and 120 rpm. Flasks were sealed with hydrophobic cotton and aluminum foil to minimize contamination while allowing gas exchange.

A range of inoculum volumes (10%–20% v/v) was tested in combination with two pulp densities: 1% w/v (2 g black mass per 200 mL) and 2% w/v. Most experiments were initiated at an adjusted initial pH of 2.0, achieved by adding H₂SO₄ depending on the medium volume. In addition, a separate set of experiments was performed without any pH adjustment, in which the natural initial pH of the 9K-black mass suspension (≈2.3–2.8) was recorded and subsequently monitored throughout the entire leaching period. This allowed systematic comparison between pH-controlled and non-adjusted conditions.

All leaching suspensions were made up to 200 mL after addition of inoculum and solid material. Incubation periods varied between 6 and 13 days depending on the tested conditions. Control tests without bacterial inoculum were conducted under identical conditions to distinguish between chemical leaching and biologically mediated dissolution. In these abiotic controls, the 9K medium (including FeSO₄·7H₂O as ferrous iron source), pulp density, initial pH adjustment protocol, temperature (30 °C), agitation rate (120 rpm), and incubation time were identical to the inoculated systems, with the sole difference being the absence of bacterial inoculation. All bioleaching and control experiments were performed in triplicate to ensure reproducibility.

2.5. Microbial Growth Monitoring

A growth curve for A. ferrooxidans was established to link bacterial activity with bioleaching performance. For this purpose, 20 mL of activated bacterial culture were inoculated into 230 mL of fresh cultivation medium in an Erlenmeyer flask and incubated at 30 °C and 120 rpm. At selected time points (0, 5, 10, 20, 30, 40, 50, 60, 70, and 80 h), about 3 mL of suspension were withdrawn and the optical density (OD) was measured at 600 nm using an DR6000 UV VIS spectrophotometer (Hach Co., Loveland, CO, USA), with the blank set to the inoculation time (t = 0 h). The OD₆₀₀ values increased from 0.014 at t = 0 to approximately 0.7 after 50 h and then stabilized, indicating that the culture had reached a stationary phase.

2.6. Bioleaching Experiments and Sampling

Bioleaching tests were carried out for total durations ranging from 6 to 13 days, depending on the experiment, with intermediate sampling to follow pH and metal recovery over time. Sampling points typically included after 1 h, 6h and daily or every second day. At each sampling time, 2 mL of leachate were withdrawn using sterile syringes, filtered through 0.22 µm syringe filters (nylon membrane, Uniflo, Whatman, Maidstone, UK), and appropriately diluted with ultrapure water before AAS analysis.

The pH of the suspensions was measured at each sampling point using a digital portable pH-meter MP125 (Mettler Toledo, Columbus, OH, USA), which was calibrated daily using standard buffer solutions. pH evolution was recorded for all experiments and used to interpret the relationship between acid production, bacterial activity, and metal dissolution.

Metal concentrations (Co, Ni, Li, Cu, Fe, Mn, Zn) in the leachates were determined by flame AAS using a VARIAN AA240FS instrument (Varian Inc., Palo Alto, CA, USA), equipped with a multi-element lamp system and an air-acetylene burner. The instrument operated over 185–900 nm, and calibration curves were prepared using external standard solutions at 0.5, 1, and 2 mg/L, diluted from certified stock standards (100 and 1000 mg/L). Τhe typical sample consumption was 6 mL/min. Lithium was quantified in emission mode, and the typical sample consumption was 3–5 mL/min. Metal recoveries (%) were calculated by comparing the dissolved metal mass in the leachate to the initial metal content in the black mass determined by digestion and AAS, taking into account the sampling volumes and dilution factors.

2.7. Post-Leaching Solid Characterization

After completion of the bioleaching experiments, solids were separated from the leachates by filtration or centrifugation. Residues were washed with ultrapure water to remove adhering solution, dried under controlled temperature and humidity conditions, and stored in sealed containers for further analysis. Dried residues were analyzed by XRD and SEM-EDS as described above, to evaluate mineralogical and microstructural changes induced by bioleaching, as well as to assess residual metal-bearing phases and graphite content.

3. Results and Discussion

3.1. Chemical Composition and Microstructure of the Black Mass

3.1.1. AAS Quantification

The results of AAS analysis, show that the black mass contains approximately 202 g/kg Co, 59.4 g/kg Ni, and 37.2 g/kg Li, with lower concentrations of Cu (14.7 g/kg), Fe (14.9 g/kg), and Mn (3.5 g/kg). These values are characteristic of LCO-based cathode materials and confirm cobalt as the dominant economically valuable metal, followed by Ni and Li. This composition is consistent with LCO-based cathode chemistries and with reported black mass compositions from industrial pre-treatment lines, where LiCoO₂ and LiNiO₂ coexist with graphite, current collector fragments and process-derived impurities [3,6,7,35,36]. The relatively high Co content confirms that cobalt remains the principal economic driver for the recycling of this type of LIBs, while the presence of Ni and Li justifies efforts toward their co-recovery [1,3,6,7].

3.1.2. XRF Results

XRF analysis was performed to obtain a semi-quantitative elemental profile of the inorganic fraction. The results are shown in

Table 1. XRF analysis of the black mass.

Element (Metal Oxide)	Element Concentration (%)	Metal Oxide Concentration (%)
Co (Co3O4)	19.1	26.3
Ni (NiO)	4.9	7.2
Cu (CuO)	0.8	1.0
Fe (Fe2O3)	0.8	1.2
Al (Al2O3)	0.6	1.0
Mn (MnO)	0.4	0.6
LOI	40%

, expressed both as elemental concentrations and corresponding metal oxides.

The XRF data confirm Co as the dominant metal species in the inorganic fraction, followed by Ni and Co. Li is absent from the spectrum due to its low atomic number (Z = 3), which results in low-energy X-ray emission that lies below the detector’s sensitivity. Notably, the Co concentration measured by XRF (19.1 wt%) aligns closely with the AAS-derived value (20.2 wt%), and the Co:Ni ratios obtained by both methods (XRF ≈ 3.8; AAS ≈ 3.4) show strong agreement. This reinforces the reliability of the combined analytical approach. The 40% LOI reported in Table 1 corresponds to moisture, graphite, polymeric binders, carbonates, hydroxides, and other volatile or combustible species. After removal of this volatile fraction, approximately 60% of the black mass is inorganic and metal-bearing, consistent with thermally pre-treated LIB black mass reported in the literature.

3.1.3. XRD Analysis of the Black Mass

The crystalline phases present in the spent LCO-derived black mass were identified by XRD (Figure S1a). Analysis reveals distinct reflections associated with the active cathode materials LiCoO₂ and LiNiO₂, as well as the anode material graphite, and minor contributions from metallic current-collector components. LiCoO₂ is characterized by a prominent peak at 2θ ≈ 19°, with additional reflections at approximately 37.5°, 39.5°, 45.3° and 49.5°, whereas LiNiO₂ exhibits its primary peak at 18.8° alongside secondary reflections at 36.9°, 38.9° and 44.5°. The higher intensity of LiCoO₂ peaks compared with LiNiO₂ is consistent with the compositional data (Table 1), confirming that cobalt-bearing phases dominate the cathode fraction. However, the presence of well-defined LiNiO₂ reflections confirms that the investigated material represents a cobalt-dominant mixed layered oxide cathode system rather than a strictly pure LiCoO₂ phase.

Both LiCoO₂ and LiNiO₂ exhibit characteristic diffraction features of layered rhombohedral R3ˉm structures, which are typical for stoichiometric and Li-deficient layered lithium transition-metal oxides used in commercial LIBs. The most intense reflection in the diffractogram occurs at 2θ ≈ 26.6°, corresponding to the (002) plane of graphite, reflecting the high abundance of graphitic carbon originating from the anode. Additional graphite reflections at 38.9°, 44.6° and 54.7° confirm the presence of a highly crystalline hexagonal graphite phase. The dominance of the graphite peak is expected given that pyrolyzed industrial black mass retains anode carbon almost quantitatively. Weak reflections attributable to Cu and Al were also detected, originating from fragmented current collectors, an observation consistent with industrial pre-treatment studies of LCO-derived battery waste [7,35,36].

The XRD patterns of the bioleached residues reveal pronounced changes compared to the initial black mass (Figure S1b). The most intense diffraction peak, located at approximately 26° (2θ), is attributed to graphite, originating from the black mass and remaining in the solid residue after bioleaching. However, the reduced apparent intensity of this graphite reflection relative to the initial material is likely not due to graphite dissolution, but rather to (i) surface coverage or partial encapsulation of graphite particles by secondary precipitates and (ii) an increase in the amorphous fraction of the residue, which is reflected by an elevated background and increased noise in the diffractogram. In addition, several diffraction features indicate the presence of hydrated iron sulfate phases in the residue. These are evidenced by a characteristic doublet around 28–29° (2θ), as well as additional reflections near 15° and 17° (2θ). The formation of such Fe-sulfate precipitates is consistent with bioleaching conditions and can significantly affect the relative intensities of crystalline phases by partially masking underlying reflections, including those of graphite. Notably, cobalt oxide phases are not detected in the bioleached residue. This absence is attributed to the effective dissolution of cobalt-containing phases during bioleaching. Any remaining cobalt-bearing compounds are expected to be present only in trace amounts, below the detection limit of XRD. Overall, the XRD results indicate that bioleaching leads to the selective removal of metal-bearing phases, while the solid residue is dominated by graphite and secondary iron sulfate precipitates with a partially amorphous character. Such behavior is well documented in biohydrometallurgical leaching of LCO-based cathodes at Fe-rich conditions [6,9,14,20,23,26].

3.1.4. SEM-EDS Microstructural Analysis

Representative SEM images of the untreated black mass (Figure 1a–c) reveal a heterogeneous assemblage of angular, irregularly shaped particles embedded within a graphite-rich matrix. EDS spot analyses confirm the presence of Co-rich and Ni-rich grains corresponding to residual cathode coatings, as well as Cu-rich fragments associated with shredded current collector foils. The mixture of particle morphologies and compositions is characteristic of pyrolyzed industrial black mass, where mechanical liberation is incomplete and composite particles persist.

Following bioleaching, significant morphological changes are evident in the solid residues (Figure 1d–f). Surfaces of Co- and Ni-bearing particles appear etched, displaying increased roughness and porosity. Many particles exhibit partial dissolution fronts, consistent with oxidative removal of metal oxides. In parallel, graphite lamellae appear cleaner and more exposed, reflecting the preferential dissolution of active cathode phases while the carbon matrix remains largely intact.

EDS spectra of leached particles show a marked reduction in Co and Ni signals, with a corresponding relative enrichment of C, further confirming selective leaching of metal oxides. This microstructural evolution is advantageous for downstream processing, as it facilitates the physical separation, purification, or potential direct reuse of the recovered graphite fraction. Similar transformations during microbial or chemical leaching of spent LIBs have been widely reported and are considered beneficial for integrated recycling schemes [20,26,36,43].

3.2. Growth Behavior of A. ferrooxidans and Implications for Bioleaching

The growth curve of A. ferrooxidans in the modified 882 medium is shown in Figure 2. After inoculation, the culture exhibited a short lag phase, followed by a rapid increase in OD₆₀₀ from 0.014 to approximately 0.7 within 50 h, after which the optical density stabilized, indicating entry into the stationary phase. This behavior is typical of iron-oxidizing acidophiles, where cell growth is tightly coupled to the oxidation of Fe²⁺ to Fe³⁺ and to the availability of dissolved oxygen [20,26,27,41].

The timing of the exponential growth phase is particularly relevant for the bioleaching experiments, since it coincides with the period of most intense Fe²⁺ oxidation and ferric iron regeneration. Operating the leaching tests at 30 °C and pH 2.0 ensures that the bacterium remains close to its optimal growth window [27,31,34,44]. The inoculum volumes employed in this study corresponding to 10%–20% v/v) thus provided a range of initial cell densities high enough to rapidly establish an active Fe²⁺-oxidizing population while allowing evaluation of the effect of biomass load on leaching performance.

3.3. Effect of Inoculum Volume at 1% Pulp Density

The influence of inoculum volume on metal dissolution was assessed at a pulp density of 1% w/v (2 g black mass per 200 mL) and an initial pH of 2.0. Figure 3a–c presents the dissolution profiles of Co, Ni, Li and Cu for inoculum volumes of 10, 15 and 20% v/v, respectively, while Figure 3d illustrates the effect of increasing pulp density to 2% at 20% v/v inoculum. In the corresponding abiotic control experiments conducted without bacterial inoculation, negligible metal dissolution was observed under otherwise identical conditions, indicating that chemical leaching by the acidic Fe²⁺-containing medium alone was minimal. This confirms that the significantly higher recoveries observed in the inoculated systems are primarily attributable to biologically mediated Fe²⁺ oxidation and subsequent ferric iron-driven indirect dissolution.

At 10% v/v inoculum (Figure 3a), metal dissolution proceeded progressively over time, with most metals showing a pronounced increase up to day 6, followed by a slight additional increase by day 7. After 6–7 days, recoveries reached approximately 60%–65% for Co, 55%–60% for Ni, 50%–55% for Li, and 90% for Cu, indicating efficient solubilization of readily accessible metal-bearing phases.

Increasing the inoculum volume to 15% v/v (Figure 3b) resulted in moderately enhanced dissolution kinetics for all metals, particularly during the early stages of leaching. Final recoveries after 7 days increased to approximately 65%–70% for Co, 60%–65% for Ni, 70%–75% for Li, and 80%–85% for Cu. Li exhibited the most pronounced improvement with increasing inoculum volume, suggesting a strong dependence on microbial activity and acid generation.

At 20% v/v inoculum (Figure 3c), metal recoveries followed a similar temporal trend, with rapid dissolution up to day 6 and marginal gains thereafter. Final recoveries after 7 days were comparable to those obtained at 15% v/v, reaching approximately 60%–65% for Co, 55%–60% for Ni, 75%–80% for Li, and 80%–85% for Cu. The limited improvement relative to 15% v/v indicates diminishing returns at higher inoculum loadings, likely due to increased competition for ferrous iron, oxygen limitation, or metal toxicity effects.

Overall, these results indicate that moderate inoculum volumes (10%–15% v/v) are sufficient to sustain effective Fe²⁺ oxidation and metal dissolution at 1% pulp density. Further increases in inoculum volume do not lead to proportional gains in recovery and may impose unnecessary biomass demand. Similar trends have been reported in other bioleaching studies of spent LIBs, where higher inoculum densities accelerate early leaching but have a limited effect on final metal recoveries [20,23,25,26,27,34,37,43].

3.4. Effect of Pulp Density

The influence of pulp density on bioleaching performance was evaluated by increasing the solids loading from 1% to 2% w/v (2 to 4 g black mass per 200 mL) while maintaining a constant inoculum volume (20% v/v) and initial pH (2.0). The corresponding dissolution profiles are shown in Figure 3d, with results at 1% pulp density provided for comparison in Figure 3a–c.

At 2% pulp density, all target metals exhibited slower dissolution rates and substantially lower final recoveries than those obtained at 1%. After 6–7 days of leaching, Co recovery decreased from approximately 64%–70% at 1% pulp density to 35%–45%, while Ni and Li recoveries were reduced to similar extents. Copper dissolution was likewise inhibited, with final recoveries remaining below those observed under lower solids loading. The consistently lower slopes of the recovery curves in Figure 3d indicate that the inhibition occurs throughout the leaching period rather than only at later stages.

This behavior reflects the intrinsic limitations imposed by higher solids loading in batch bioleaching systems. Increasing the pulp density raises the concentration of dissolved metals in the leachate, which can suppress microbial activity and slow ferric iron regeneration through inhibitory effects on A. ferrooxidans [20,26,31,34]. Simultaneously, the amount of ferrous iron supplied by the 9K medium becomes insufficient relative to the increased mass of solid, reducing the availability of ferric iron required for indirect oxidative dissolution. Higher pulp density also increases slurry viscosity and particle-particle interactions, which can impair oxygen transfer and limit effective contact between the biogenic lixiviants and metal-bearing phases.

Comparable reductions in bioleaching efficiency with increasing pulp density have been widely reported for spent LIB black mass, with most batch studies identifying optimal solids loadings at or below 1%–2% w/v to balance metal recovery and microbial stability [20,23,25,26,28,29,43,44]. The results obtained here are therefore consistent with literature trends and highlight pulp density as a critical design parameter that must be carefully controlled when translating bioleaching processes from laboratory to larger-scale systems.

3.5. Influence of Initial and Dynamic pH Evolution on Bioleaching Performance

To elucidate the role of pH in controlling microbial activity and metal dissolution, bioleaching experiments were conducted either with initial pH adjustment to 2.0 or without adjustment, allowing the natural pH of the 9K-black mass suspension (≈2.3–2.8) to evolve freely. The temporal variation in pH during representative experiments is shown in Figure 4, corresponding to tests performed at 1% pulp density with inoculum volumes of 10% v/v (Π.1.5), 15% v/v (Π.1.10) and 20% v/v (Π.1.20).

In all pH-adjusted experiments, a characteristic pH profile was observed. During the first 2–3 days, pH increased slightly, reaching values around 3.0–3.3, reflecting initial buffering by the black mass and partial consumption of acidity during early metal dissolution. This was followed by a pronounced decrease in pH, reaching minimum values of approximately 1.5–1.6 for Π.1.5, ~1.9 for Π.1.10, and as low as ~0.9 for Π.1.20 around days 5–6. The subsequent gradual increase and stabilization of pH toward the end of the experiments (days 9–13) indicate partial neutralization as readily leachable phases were depleted and the rate of acid generation slowed.

This pH evolution is consistent with the indirect bioleaching mechanism mediated by A. ferrooxidans, in which oxidation of Fe²⁺ to Fe³⁺ and reduced sulfur compounds generates sulfuric acid, while ferric iron is simultaneously consumed during reductive dissolution of LiCoO₂ and LiNiO₂ phases [20,23,27,41,49]. The lowest pH values coincided with the period of most intense metal dissolution, indicating that acidification and ferric iron regeneration act synergistically to control leaching kinetics.

The magnitude of pH decrease was strongly dependent on inoculum volume. At 20% v/v inoculum, rapid establishment of an active microbial population led to accelerated acid generation and the lowest pH values, whereas lower inoculum volumes resulted in more moderate acidification. This behavior explains the faster initial dissolution observed at higher inoculum loadings, but also highlights the potential for excessively low pH to enhance metal toxicity or destabilize microbial activity over extended periods.

Experiments conducted without initial pH adjustment followed a similar qualitative trend but exhibited a more gradual acidification and did not reach the extremely low pH values observed in the adjusted systems. Under these conditions, final recoveries of Co, Ni and Cu remained comparable to those obtained at initial pH 2.0, demonstrating that A. ferrooxidans is capable of self-acidifying the system to levels sufficient for effective dissolution. Notably, Li recovery was consistently enhanced in the non-adjusted experiments, reaching values up to ~79%, suggesting that slightly higher pH conditions may limit Li reprecipitation and favor proton-lattice exchange reactions [20,23,26,33,43].

The close correspondence between pH minima and the steepest increases in metal recovery confirms that pH evolution is a central process variable governing bioleaching efficiency, rather than a passive parameter. Together, these results indicate that strict initial pH adjustment is not mandatory for efficient Co and Ni recovery at low pulp density, but that controlled pH trajectories can be exploited to optimize Li dissolution and balance microbial activity against metal toxicity.

Overall, the data demonstrate that both initial pH conditions and dynamic pH evolution during leaching play a decisive role in determining bioleaching performance. Similar sensitivity of LIB bioleaching systems to pH and redox conditions has been widely reported for bacterial and mixed-culture processes treating LCO- and LFP-type cathode materials [20,26,28,31].

3.6. Linking pH Evolution, Microbial Activity and Dissolution Kinetics

The combined pH trajectories (Figure 4), growth behavior (Figure 2), and dissolution curves (Figure 3) indicate that bioleaching performance was governed by the establishment of an active Fe²⁺-oxidizing population and the resulting evolution of acidity and oxidative capacity in the leaching liquor. The rapid increase in OD₆₀₀ up to ~50 h (Figure 2) marks the period during which Fe²⁺ oxidation and Fe³⁺ regeneration are expected to be most intense, supporting the indirect mechanism in which biogenic Fe³⁺ and acidity drive dissolution of LiCoO₂/LiNiO₂ phases [20,23,27,41,49]. Although redox potential (Eh) and Fe²⁺/Fe³⁺ speciation were not directly monitored during the leaching experiments, the observed pH trajectories, growth behavior, and negligible dissolution in abiotic controls are consistent with the predominance of biologically mediated ferric regeneration as the driving mechanism. Consistent with this, the steepest increases in metal recovery occurred during the interval of strongest acidification (Figure 4) and preceding the plateau observed after ~6–7 days (Figure 3), suggesting that dissolution was fastest while ferric regeneration and acidity build-up were highest. The dissolution behavior is consistent with an indirect ferric-mediated mechanism, which is recognized as the dominant pathway in iron-driven bioleaching systems. While localized bacteria-mineral interactions may occur, the highly acidic and Fe-rich conditions employed in this study strongly favor indirect redoxolysis as the primary dissolution mechanism.

As leaching progressed, recoveries approached a plateau and pH gradually stabilized, indicating a transition from an initially reaction-controlled regime (high availability of reactive surfaces and strong oxidizing conditions) toward a regime limited by reduced accessibility of remaining metal-bearing phases. Such late-stage limitations are commonly attributed to depletion of readily leachable cathode material, surface passivation by altered layers, and/or diffusion constraints within composite particles, rather than simply insufficient biomass [26,31,34]. In this context, the pH history becomes a useful proxy for process intensity: pronounced acidification indicates sustained microbial oxidation activity, whereas stabilization reflects declining net acid generation and lower effective oxidative driving force.

3.7. Post-Leaching Residue Characterization

Mineralogical and microstructural analyses indicate the selective removal of metal-bearing cathode phases, while the carbonaceous component of the black mass remains in the solid residue. The XRD patterns of the leached residues (Figure S1b) show a pronounced attenuation of LiCoO₂ and LiNiO₂ reflections, consistent with the effective dissolution of Co- and Ni-containing oxides during bioleaching. The characteristic graphite reflection at ~26° (2θ) is still observed, confirming the persistence of graphitic carbon; however, its apparent intensity is reduced relative to the initial material, rather than remaining unchanged. This reduction is attributed to partial surface coverage or encapsulation of graphite particles by secondary precipitates, as well as to an increased proportion of amorphous phases in the residue, which manifests as an elevated background and increased noise in the diffractograms. Consequently, changes in relative peak intensities reflect not only phase abundance but also microstructural and surface effects induced during leaching.

In several residues, weak reflections assignable to Fe-containing secondary phases were detected, consistent with the precipitation of hydrated iron sulfate species under acidic, Fe-rich bioleaching conditions. This interpretation is further supported by SEM-EDS analysis of representative residue areas (Supplementary Figure S2a,b and Table S1), which reveal Fe and S as the dominant elements, with Fe contents exceeding 70 wt% in localized regions. The formation of such Fe-rich secondary phases is commonly reported in iron-driven bioleaching systems and may partially mask underlying crystalline phases in XRD patterns. Notably, cobalt was detected only at trace levels (<2 wt% in analyzed spectra), supporting the substantial depletion of Co-bearing phases after bioleaching. While minor amorphous Co-containing species below XRD detection limits cannot be entirely excluded, the combined XRD and SEM-EDS results consistently indicate effective dissolution of the original crystalline cobalt oxides.

SEM imaging further corroborates these findings by revealing pronounced morphological changes. Compared with the heterogeneous, compact agglomerates of the feed (Figure 1a–c), the bioleached residues (Figure 1d–f) exhibit etched surfaces, increased porosity and partial loss of Co/Ni-rich domains. The relative exposure of graphite lamellae and enrichment of carbon signatures in EDS are consistent with preferential dissolution of metal oxides and persistence of carbon-rich phases [20,26,36,43]. This residue evolution is relevant from a process perspective because it suggests that bioleaching can serve as a conditioning step that not only solubilizes target metals but also improves the liberation and potential valorization of the graphite fraction, depending on downstream separation routes.

3.8. Comparison with Previous Bioleaching Studies and Process Implications

A direct comparison between the present results and representative bioleaching studies reported in the literature is provided in

Table 2. Comparison of selected bioleaching studies for metal recovery from spent lithium-ion batteries and the present work.

Study	Microorganism	Feed Material	Key Operating Conditions	Co (%)	Ni (%)	Li (%)	Cu (%)
Heydarian et al., 2018 [34]	Mixed acidophilic culture	Laptop LIBs (mixed cathodes)	1% pulp, pH 1.8–2.0, 30 °C, two-step	~65	~55	—	—
Nazerian et al., 2023 [37]	A. ferrooxidans (+ultrasound)	Spent LIB black mass	2% pulp, pH 2.0, 30 °C, ultrasound-assisted	68	62	71	—
Alipanah et al., 2023 [23]	A. ferrooxidans	Spent LIBs (mixed cathodes)	1% pulp, pH 2.0, 30 °C, optimized via DoE	~70	~60	~65	—
Panda et al., 2024 [25]	Mixed bacterial consortium	Industrial LIB black mass	1%–2% pulp, pH 2.0, 30 °C, scale-up tests	60–68	55–63	50–65	—
Kim et al., 2024 [47]	A. ferrooxidans + magnetic field	Spent LIB cathode material	3% pulp, pH 2.0, 30 °C, magnetic field	>80	>80	—	—
This work	A. ferrooxidans	Pyrolyzed industrial LCO black mass	1% pulp, pH 2.0/non-adjusted, 30 °C	64–70	57–72	52–79	81–100

. Under the best-performing conditions identified here (industrial LCO-derived black mass, 1% pulp density, 30 °C, 6–7 days), Co and Ni recoveries of 64%–70% and 57%–72%, respectively, fall within the upper range typically reported for single-strain Acidithiobacillus ferrooxidans systems treating complex LIB residues. Li recovery reached 52%–60% under pH-adjusted conditions and increased to approximately 79% when the system was allowed to self-acidify, highlighting the sensitivity of Li behavior to pH trajectories. Cu dissolution was consistently high (81%–100%), reflecting the high lability of current-collector-derived Cu phases in acidic, oxidizing leachates and the effectiveness of the applied pretreatment. These values are comparable to recent scale-up bioleaching studies. For example, Panda et al. [25] reported up to 81% Co, 99% Ni and 67% Li recovery at laboratory scale (1 L, 6 days), and 75% Co, 91% Ni and 80% Li at 10 L scale within 4 days under optimized conditions. Such results confirm that high Ni and moderate-to-high Co recoveries can be achieved under mesophilic bioleaching conditions, although performance remains sensitive to pulp density and microbial adaptation.

It should be emphasized that direct comparison between studies must also consider differences in cathode chemistry. The present work examines LCO-derived black mass, characterized by a layered cobalt-rich oxide structure that is particularly responsive to indirect ferric-iron-mediated dissolution. In contrast, LFP systems exhibit different leaching dynamics due to the stability of the olivine phosphate framework and the predominance of Fe rather than Co as the redox-active metal [25,33]. Similarly, mixed NMC materials may display competitive dissolution among Co, Ni and Mn, with Mn often exhibiting slower kinetics under acidic ferric-mediated conditions [20,26]. Consequently, battery composition fundamentally influences apparent recovery efficiencies and must be considered when benchmarking bioleaching performance across studies.

Compared with fungal systems and mixed microbial consortia, which often require longer residence times or higher organic acid production to achieve comparable recoveries, the present results demonstrate that a single, well-characterized iron-oxidizing bacterium can deliver competitive performance on heterogeneous, pyrolyzed industrial black mass. This is notable given that such materials are typically more impurity-rich and structurally complex than laboratory-prepared cathode powders, conditions that frequently suppress apparent bioleaching efficiency and slow dissolution kinetics.

Recent process-intensification approaches, including ultrasonic assistance and magnetic-field-enhanced bioleaching, have shown that higher recoveries or shorter leaching times can be achieved, particularly at elevated pulp densities. However, these configurations introduce additional operational complexity and energy inputs. In contrast, the present work establishes a robust baseline using a conventional shake-flask configuration and an unadapted A. ferrooxidans culture, demonstrating that substantial Co, Ni, Li and Cu recovery can be achieved under mild conditions without auxiliary intensification.

When benchmarked against conventional recycling technologies, pyrometallurgical routes remain the industrially established reference. Smelting-based processes typically operate at temperatures exceeding 1200–1500 °C and achieve near-complete transfer of Co and Ni (>99%) into a metallic alloy phase [50,51]. However, Li is predominantly partitioned into the slag phase during smelting and requires subsequent hydrometallurgical treatment for recovery [50,51,52]. Thus, while pyrometallurgy offers rapid kinetics (hours rather than days) and very high transition-metal recovery efficiencies, it involves substantial energy input and multi-step downstream processing for Li valorization [51]. In contrast, the bioleaching approach evaluated here proceeds at 30 °C and atmospheric pressure, directly solubilizing Co, Ni and Li into the aqueous phase without high-temperature partition losses of Li. Although dissolution kinetics are slower and overall Co recovery remains below that achieved by smelting, bioleaching offers potential advantages in terms of lower energy intensity, selective metal solubilization via pH and redox control, and simplified integration into hydrometallurgical recovery flowsheets.

Despite demonstrating technical feasibility, several challenges must be addressed before industrial-scale implementation can be realized. A primary limitation concerns pulp density. As shown in this study, increasing solids loading from 1% to 2% significantly reduced metal recoveries, likely associated with microbial inhibition, increased dissolved metal toxicity, and reduced ferric iron availability relative to the solid mass. Similar inhibition at elevated pulp density was reported by Panda et al. [25], who observed decreased microbial activity at 1% solids and consequently operated at 0.5% pulp density. Likewise, Roy et al. [20] conducted bioleaching at low pulp density (0.1%), highlighting the operational limitations of iron-oxidizing systems when treating LIB materials. Industrial implementation will therefore require strategies to mitigate toxicity and maintain microbial stability at higher solids loadings.

In addition, oxygen transfer and mixing efficiency represent critical constraints in larger bioreactors [53]. Iron oxidation by A. ferrooxidans is strictly aerobic, and insufficient oxygen supply can limit ferric iron regeneration, thereby reducing oxidative dissolution rates [41]. At higher solids loadings, increased slurry viscosity and particle interactions may further impair mass transfer and redox cycling [33,53]. Elevated dissolved metal concentrations (particularly Co²⁺ and Ni²⁺) have been reported to suppress microbial activity and limit ferric iron regeneration in iron-oxidizing bioleaching systems [54]. Consequently, careful process control, including monitoring of redox potential Eh), pH evolution, and iron speciation, will be essential during scale-up [54]. Reactor configuration must also be optimized, with evaluation of stirred tank, airlift, or continuous-flow systems to improve oxygen distribution and redox stability compared to simple batch shake-flask operation [55]. Addressing these scale-dependent constraints will be central to translating laboratory bioleaching performance into industrial application.

From a process perspective, the observed dissolution plateau after approximately 6–7 days suggests that staged leaching, liquor renewal or continuous operation may further enhance overall recovery by sustaining ferric iron regeneration and limiting late-stage inhibition. The strong dependence of performance on pulp density and pH evolution reinforces the need for careful control of solids loading, redox balance and acidification pathways during scale-up. Overall, these findings confirm the technical feasibility of A. ferrooxidans-assisted bioleaching for industrial LCO black mass and provide clear operational windows for subsequent optimization and integration into circular recycling flowsheets for spent lithium-ion batteries.

4. Conclusions

This study demonstrates the technical feasibility of bioleaching critical metals from pyrolyzed industrial LiCoO₂-derived black mass using Acidithiobacillus ferrooxidans under mild mesophilic conditions (30 °C). At 1% pulp density, substantial metal recoveries were achieved within 6–7 days, reaching 64%–70% for Co, 57%–72% for Ni, 52%–60% for Li (increasing up to ~79% without initial pH adjustment), and 81%–100% for Cu. The dissolution profiles indicate that most metal solubilization occurred during the first six days of operation, followed by a plateau phase, suggesting depletion of readily accessible metal-bearing phases and/or emerging kinetic limitations such as surface passivation or diffusion constraints.

The evolution of pH and microbial growth behavior confirms that leaching performance is strongly governed by the establishment of an active iron-oxidizing population and the development of sufficiently acidic and oxidizing conditions in the leachate. Increasing pulp density from 1% to 2% significantly reduced dissolution rates and final recoveries, identifying solids loading as a primary operational constraint in batch bioleaching systems. While strict initial pH adjustment was not essential for achieving high Co and Ni recoveries at low pulp density, the pH trajectory influenced lithium behavior, highlighting the importance of dynamic pH management when Li co-recovery is targeted. Mineralogical and microstructural analyses confirmed the selective dissolution of Co- and Ni-bearing oxides, while graphite remained in the solid residue together with Fe-rich secondary precipitates. This selective behavior suggests that bioleaching may also facilitate downstream separation or valorization of the carbonaceous fraction.

The results define clear operational windows for optimizing bacterial bioleaching of industrial LCO-derived black mass and provide quantitative benchmarks for process development. From a scale-up perspective, future work should focus on increasing pulp density tolerance, improving oxygen transfer and ferric iron regeneration under higher solids loading, mitigating dissolved metal toxicity, and evaluating continuous or semi-continuous reactor configurations. Addressing these challenges will be essential for translating laboratory-scale bioleaching into an industrially viable and low-impact recycling route for spent lithium-ion batteries.