Hydrometallurgical Production of Electrolytic Manganese Dioxide (EMD) from Furnace Fines

The ferromanganese (FeMn) alloy is produced through the smelting-reduction of manganese ores in submerged arc furnaces. This process generates large amounts of furnace dust that is environmentally problematic for storage. Due to its fineness and high volatile content, this furnace dust cannot be recirculated through the process, either. Conventional MnO2 production requires the pre-reduction of low-grade ores at around 900 °C to convert the manganese oxides present in the ore into their respective acid-soluble forms; however, the furnace dust is a partly reduced by-product. In this study, a hydrometallurgical route is proposed to valorize the waste dust for the production of battery-grade MnO2. By using dextrin, a cheap organic reductant, the direct and complete dissolution of the manganese in the furnace dust is possible without any need for high-temperature pre-reduction. The leachate is then purified through pH adjustment followed by direct electrowinning for electrolytic manganese dioxide (EMD) production. An overall manganese recovery rate of >90% is achieved.


Introduction
Manganese is an important raw material for steelmaking, batteries, fertilizers, catalysts, pigments, and non-ferrous alloys [1]. Manganese is the third most common constituent of steel, which is used as both a deoxidizer and an alloying agent. Typically, 7-10 kg of manganese-based ferroalloys (FeMn alloys) are required per ton of steel production [2]. Steelmaking, including its iron-making component, consumed more than 90% of mined manganese ores in 2013 [3].
Manganese dioxide (MnO 2 ) occurs in nature as the mineral pyrolusite, which is about 62-63% manganese. The most important use of MnO 2 is in primary Leclanché (carbon-zinc) and alkaline batteries. This material is used in obtaining the spinel structure of the cathode materials to be used in rechargeable Li-ion batteries (e.g., LiMn 2 O 4 ) [4][5][6]. MnO 2 needed for the production of batteries must have high purity and high electrochemical activity. Among its several allotropic forms, electrochemical activity is the highest for γ-MnO 2 . Hence, it is the best material for battery applications [7].
Since the early 2000s, the steady growth in demand for manganese dioxides has come from primary and secondary battery industries [8,9]. Three groups of manganese dioxides are being used in energy storage devices-namely natural (NMD), chemical (CMD), and electrolytic (EMD) manganese dioxide. The first type has been used in standard or Leclanché cells, whereas modern batteries, such as alkaline and lithium batteries, require the two synthetic forms with improved properties.
In terms of alkaline batteries, the use of EMD within the industry has exceeded 230,000 metric tons per annum, with a growth rate of about 10% annually [7]. With increasing global demand for batteries, the annual growth rate is expected to rise in the future. An additional increase in the demand for EMD is expected from the secondary, or rechargeable, battery market. This is mainly because lithium manganese ion batteries that use EMD in their manufacturing are replacing cobalt-type batteries as the cheaper and greener alternative. Manganese is being considered as a potential replacement for cobalt in the cathode material of lithium-ion batteries since it can increase safety and reduce cost, and it is environmentally more benign [10]. Growth is also likely to come from the use of EMD in hybrid electric vehicles [11].
It is possible to use a manganese ore to directly manufacture batteries so long as it meets specific characteristics and composition. This type of manganese dioxide is known as natural manganese dioxide, or NMD [12]. However, the demand for this material cannot be fulfilled through fresh ore only. The minimum and maximum concentrations for an ore suitable for Leclanché battery production is roughly 75-85 wt.% for MnO 2 with 3-5 wt.% H 2 O, 0.5-5 wt.% SiO 2 , 0.2-0.3 wt.% Fe, and 0.1-0.2 wt.% for other metal oxides [13]. However, in alkaline, lithium, and other modern batteries, synthetic manganese dioxide with improved purity and quality becomes a must; therefore, it is necessary to produce it through chemical (CMD) or electrochemical (EMD) processes.
Conventionally, synthetic manganese dioxide is mainly produced from pyrolusite (MnO 2 ) or rhodochrosite (MnCO 3 ) ores. Pyrolusite ore has to be reduced before leaching, or it can be directly leached through a reductive leaching process [14]. After leaching and filtration, the leach liquor contains a variety of impurities, such as alkali metals, iron, nickel, and so on. Most of the iron present in the solution is removed through goethite precipitation by increasing the pH of the leachate to 2-3 with the addition of lime. Potassium and the rest of the iron are removed through further lime addition to maintain a pH level between 4-6 (i.e., jarosite precipitation). Mn does not precipitate until pH > 7 [15]. Ni, Cu, Mo, and other impurities that do not precipitate like Mn are removed through sulfide precipitation by adding Na 2 S or B 2 S [7]. After these purification steps, the manganese sulfate solution is forwarded to the electrochemical (for EMD) or chemical (for CMD) production step. The electrolysis process is more advantageous, as it produces MnO 2 with better properties, regenerates acid, uses a smaller number of reagents, and generates fewer residues that may be harmful to the environment [7,12,[16][17][18]. In EMD production, a purified leach solution containing around 150 g of MnSO 4 /L is used. Cell reactions are given in Equations (1)-(3) [19]. The voltammogram of EMD production exhibits an anodic current peak at about 1.3 V vs. SCE (MnO 2 deposition), while a cathodic peak appears at 0. 8 Furnace dust is a problematic by-product of the ferromanganese (FeMn) and silicomanganese (SiMn) industries. Its storage is a long-term environmental concern, as it requires efficient technologies for its recycling [19]. The furnace dust contains high concentrations of manganese oxides, with up to 40% or more concentrate [20]. The recycling of the dust back into the ferroalloy furnaces would not only reduce that environmental liability but also decrease the fresh ore consumption. Unfortunately, this is not possible due to the high volatile content of furnace dust, along with its fineness. Many manganese ores contain substantial amounts of potassium (up to 2-3%). Much of this volatilizes and reports to the fume during the smelting operation [20]. The concern regarding the recycling of the fume is that volatile transition metals, such as zinc, can build up due to repeated recycling. One of Elkem's submerged arc furnaces producing high carbon FeMn alloy had a severe eruption on December 9, 1992, due to an accumulation of volatiles which caused unstable structure formations in the furnace [21].
There is limited literature on the topic of recycling FeMn or SiMn furnace fines for manganese recovery, particularly through hydrometallurgical treatments. Nkosi et al.
(2011) obtained a 49% Mn recovery rate from SiMn submerged arc furnace dust through direct atmospheric leaching using a diluted sulfuric acid solution [22]. de Arujo et al. (2006) studied the replacement of rhodochrosite ore by ferromanganese fines for the production of EMD [19]. The fines were directly digested in high concentrations of sulfuric acid, and the resultant solution was purified through pH adjustment first using NH 3 (for iron removal) and then using a Na 2 S addition (for heavy metal removal). However, the study is mostly focused on the electrodeposition behavior of the purified digestion solution, with very little insight into the previous steps. Shen et al. (2007) and Hamano et al. (2008) proposed recycling routes for different dust samples generated by FeMn and SiMn production [23,24]. However, both studies only focus on the recovery of zinc that constitutes ≤1.5% of the dust. In this study, an alternative hydrometallurgical process is proposed for the utilization of FeMn furnace dust in the production of high purity electrolytic manganese dioxide (EMD). An experimental comparison is made between direct reductive leaching of the fines, using a novel, cheap, and green organic, and direct acid leaching.
It should be noted that, unlike the ores, the furnace dust is already in fine sizes, thus rendering the costly particle size reduction steps unnecessary. Its use to replace rhodochrosite (MnCO 3 ) and pyrolusite (MnO 2 ) for EMD production has other advantages too.
The concentrations of some undesirable impurities, such as Ni, Cu, and Mo, are smaller in the furnace dust than they are in the rhodochrosite ore. Although K and Na contents are significantly higher in the furnace dust, these elements do not affect the manganese dioxide electrodeposition. Furthermore, such fines do not generate CO 2 , which is formed through the reaction of carbonate present in the rhodochrosite ore.
In comparison to the pyrolusite ore, the furnace dust is already partially reduced during its formation. This means direct reductive leaching of the furnace dust is more beneficial, as less of the reductant will be needed than is needed for the ore. Compared to their inorganic counterparts, organic reductants are more preferable due to their environmentally friendly nature. Soluble organic compounds are the most suitable, compared to insoluble organic compounds, due to their faster reactivity. Sugar and glucose were found to be the most promising reductants [25]. However, in this study, dextrin-a water-soluble, organic reductant-is investigated as the cheaper organic alternative over sugar or glucose. The produced leachate is then purified conventionally, and the subsequent solution is used for conventional EMD production.

Materials and Methods
The furnace dust used in this study was obtained from the Ferro Alloy Plant (FAP) of Tata Steel in Joda, India. The entire sample was collected over a period of time in order to have an average chemical composition and phase distribution that might have varied by short-term differentiations in the furnace input materials. After sieved to −1 mm size, the entire sample was mixed thoroughly before preparing a representative sample. A part of the representative sample was taken for analyses using a coning and quartering technique. Chemical grade sulfuric acid, dextrin, and slaked lime (Ca(OH) 2 ) were used in the present study.
A particle size analysis was carried out with the help of the wet sieving method. The chemical analysis of the samples was performed using a Spectro Analytical Instruments, Ciros model, inductively coupled plasma-optical emission spectrometer (ICP-OES) (SPEC-TRO Analytical Instruments Inc., Clive, Germany). The mineral phases of the samples were identified using a Panalytical X'pert Pro X-ray diffractometer (XRD) (Malvern Panalytical Ltd., Malvern, UK). The experimental parameters for XRD analysis were: 20-90 2-theta degree; radiation of CuKα; acceleration voltage of 40 kV; acceleration current of 30 mA; with a step size of 0.020 degrees. The phases present in the samples were also examined using a JEOL (Tokyo, Japan), an 840A model scanning electron microscope (SEM), equipped with an energy-dispersive X-ray detector (EDX).

Leaching Experiments
Leaching was performed in a conical flask on a magnetic stirrer that was fixed at 200 rpm throughout the study. 10 g of the dust sample was used in each experiment with a fixed solid: liquid ratio of 1:5 wt./vol. The acid amount was varied between 1M (8%) and 3M (24%). The dust sample was slowly added to the acidic solution with or without a reductive agent. The slow addition was due to the vigorous nature of the exothermic leaching reaction amplified by the fine particle size of the dust. To avoid material and heat loss, the flask was covered with aluminum foil or a watch glass throughout the leaching duration. The studied parameters and their ranges are summarized in Table 1. After the leaching duration was completed, the solution was allowed to cool down. The sludge was rather gelatinous and hard to filter, possibly due to the presence of orthosilicic acid. The cooled solution was treated with lime addition to ease the filtration, which also helped neutralize the excess acid and remove the impurities. The lime-treated solution, with a pH of around 6, was quickly filtered with a funnel and filter paper. Since Mn precipitation does not occur up to pH 7-8, the loss of Mn to precipitation was minimal and was included in the overall Mn recovery rate [15]. The residue was washed 5 to 6 times to remove all the soluble manganese compounds. This final solution was used for electrolysis experiments.

Electrolysis Experiments
The electrolysis experiments were carried out in a cell consisting of a 250 mL beaker on top of a heating plate, two counter electrodes, one anode, a thermometer, and a DC power supply. Graphite was used for both electrodes. The cathode dimensions were 5 cm length, 1 cm width, and 0.1 cm thickness. The anode dimensions were 5 cm length, 2 cm width, and 0.1 cm thickness.
The electrolyte was prepared from purified leach solution and sulfuric acid. The solution temperature was maintained at 92 • C (±2 • C). The volume of the electrolyte was maintained through water addition during the experiment. The anode and counter electrodes were partially submerged in the electrolyte in order to maintain anode to cathode surface ratio of 2:1. After closing the cell, the synthesis of MnO 2 was carried out with the help of a DC power supply. No external stirring was needed, as the hydrogen gas generated during the process created sufficient stirring in the solution.
Electrolysis was carried out at different current densities and acid concentrations to optimize the current efficiency. Different current densities (i.e., 0.5, 1, 1.5, 2, and 2.5 amp/dm 2 ) were used with 0.5 mol of MnSO 4 and 0.25 mol of acid-containing electrolytes. In the other set of experiments, different H 2 SO 4 concentrations (from 0.05 to 0.45 M, with 0.1 intervals) were used. In all experiments, the electrolysis duration was fixed to 1 h. The weight of MnO 2 deposited on the anode was noted after each experiment.

Characterization of Furnace Dust
The chemical analysis of the furnace dust used in the present study is provided in Table 2, and shows that the major constituents of the sample are Mn-and Si-based compounds. The XRD pattern of the furnace dust in Figure 1 shows three main compoundsnamely, hausmannite (Mn 3 O 4 ), manganosite (MnO), and silica (SiO 2 ). The SEM micrograph of the furnace dust sample in Figure 2 shows that most of the furnace dust is less than 10 microns. The spot and area analysis indicated the presence of alkali metals, such as sodium, potassium, and barium. The chemical analysis of the furnace dust used in the present study i Table 2, and shows that the major constituents of the sample are Mn-and pounds. The XRD pattern of the furnace dust in Figure 1 shows three main c namely, hausmannite (Mn3O4), manganosite (MnO), and silica (SiO2). Th graph of the furnace dust sample in Figure 2 shows that most of the furna than 10 microns. The spot and area analysis indicated the presence of alkal as sodium, potassium, and barium.
A cumulative particle size analysis of the sample using the wet sie showed that >90% of the sample was less than 37 microns, and D80 of the s microns. This shows that the furnace dust sample was such a fine materia grinding would be simply redundant.

Characterization of Furnace dust
The chemical analysis of the furnace dust used in the present study is pro Table 2, and shows that the major constituents of the sample are Mn-and Si-bas pounds. The XRD pattern of the furnace dust in Figure 1 shows three main comp namely, hausmannite (Mn3O4), manganosite (MnO), and silica (SiO2). The SEM graph of the furnace dust sample in Figure 2 shows that most of the furnace du than 10 microns. The spot and area analysis indicated the presence of alkali met as sodium, potassium, and barium.
A cumulative particle size analysis of the sample using the wet sieving showed that >90% of the sample was less than 37 microns, and D80 of the sampl microns. This shows that the furnace dust sample was such a fine material tha grinding would be simply redundant.     A cumulative particle size analysis of the sample using the wet sieving method showed that >90% of the sample was less than 37 microns, and D 80 of the sample was 32 microns. This shows that the furnace dust sample was such a fine material that further grinding would be simply redundant.

Leaching Experiments Without Reductant Addition (Direct Acid Leaching)
In the first part of the experiments, leaching was conducted without a reductant, at different leaching temperatures and acid concentrations, for a 1 h duration. The obtained results are provided in Figure 3a. The Mn dissolution rate increases to about 50% when the acid concentration is increased to 12%; however, it becomes stagnant thereafter, with a <10% increase at the highest acid concentration studied (20%). Meanwhile, manganese dissolution slightly increases with an increase in the leaching temperature. This may be due to the faster reaction of Mn with acid.
due to the presence of Mn3O4 and MnO2 in the furnace dust sample. The Mn with sulfuric acid is provided in Equation (4). From this reaction, it can be co two parts of Mn3O4 present in the dust sample are soluble, and one part is in is because the MnO2 present in the dust is completely insoluble in the sulfu tion. This explains why the overall Mn recovery is less than 60%.
Mn3O4 + 2H2SO4 = 2MnSO4 + MnO2 + 2H2O The effect of leaching duration on Mn dissolution was studied at differen vals from 15 to 60 min, a 12% acid concentration, and a 30°C leaching temper 3b shows that, after the first half an hour, the dissolution rate of Mn reaches of about 48% and becomes stable despite the very fine particle size of the improves the leaching kinetics. The optimized conditions for direct leach found at a 30°C leaching temperature, a 12% acid concentration, and a 30 m duration. The XRD analysis of the residue is provided in Figure 4. Only the silica phases are clearly detectable. The calcium oxide present in the sample reac sulfuric acid to create insoluble gypsum. There is no clear indication of an The initial drastic increase in the Mn dissolution rate is due to an increase in the availability of sulfuric acid. However, at higher acid concentrations, there is barely any soluble manganese form left. In all experiments, the Mn dissolution rate is less than 60%. This is due to the presence of Mn 3 O 4 and MnO 2 in the furnace dust sample. The Mn 3 O 4 reaction with sulfuric acid is provided in Equation (4). From this reaction, it can be concluded that two parts of Mn 3 O 4 present in the dust sample are soluble, and one part is insoluble. This is because the MnO 2 present in the dust is completely insoluble in the sulfuric acid solution. This explains why the overall Mn recovery is less than 60%. The effect of leaching duration on Mn dissolution was studied at different time intervals from 15 to 60 min, a 12% acid concentration, and a 30 • C leaching temperature. Figure 3b shows that, after the first half an hour, the dissolution rate of Mn reaches a maximum of about 48% and becomes stable despite the very fine particle size of the sample that improves the leaching kinetics. The optimized conditions for direct leaching are then found at a 30 • C leaching temperature, a 12% acid concentration, and a 30 min leaching duration.
The XRD analysis of the residue is provided in Figure 4. Only the silica and gypsum phases are clearly detectable. The calcium oxide present in the sample reacted with the sulfuric acid to create insoluble gypsum. There is no clear indication of any Mn-based compounds (e.g., MnO 2 ) in the XRD pattern. However, the fresh and acid-insoluble MnO 2 produced through the partial dissolution of Mn 3 O 4 during leaching can still be present in the residue. Synthetic MnO 2 typically has low-intensity and broad characteristic peaks [15]. Along with the fineness of the furnace dust that promotes the background noise, it is very likely that the amorphous and weak peaks of MnO 2 that partly coincide with those of gypsum are dwarfed by the stronger peaks of the two crystalline phases. compounds (e.g., MnO2) in the XRD pattern. However, the fresh and acid-insoluble MnO2 produced through the partial dissolution of Mn3O4 during leaching can still be present in the residue. Synthetic MnO2 typically has low-intensity and broad characteristic peaks [15]. Along with the fineness of the furnace dust that promotes the background noise, it is very likely that the amorphous and weak peaks of MnO2 that partly coincide with those of gypsum are dwarfed by the stronger peaks of the two crystalline phases.

Leaching with Reductant Addition (Direct Reductive Leaching)
Through direct acid leaching experiments, it was found that maximum recovery of the manganese is less than 60% without any addition of a reductant. This is most likely due to the involvement of MnO2, which can only be effectively dissolved in sulfuric acid in a reducing atmosphere. In the second part of the leaching experiments, dextrin was added as the reductant. The amount of dextrin required for the complete reduction of manganese dioxide was calculated according to the reaction in Equation (5). Around 50% of the Mn present in the dust sample is soluble in acid without any reductant. Hence, the other half requires a reductant. Then, the stoichiometric need for dextrin was calculated as 0.05 g/g of dust (or 5% dextrin). However, for the initial studies, 50% excess or 0.08 g/g of dust (or 8% dextrin) was used to ensure sufficient dextrin presence. It should be noted that the reduction of MnO2 by dextrin (or the oxidation of dextrin by MnO2) is most likely not a single-step reaction. Previous studies showed that the acid leaching of the pyrolusite ore (MnO2) in the presence of carbohydrates, such as glucose (C6H12O6), lactose (C12H22O11), and sucrose (C12H24O11), results in intermediate reactions that provide intermediate degradation products, such as HCOOH and HCHO [25][26][27]. Based on this information, it is very likely that the same is valid for the case of dextrin, another carbohydrate.
12MnO2 + C6H10O5 + 12H2SO4 = 12MnSO4 + 17H2O + 6CO2 (5) Figure 5a shows the effect of the leaching temperature and acid concentration on Mn dissolution in the presence of dextrin. To ensure that the amount of acid is sufficient in the case of a possible complete Mn dissolution, these experiments were conducted at more

Leaching with Reductant Addition (Direct Reductive Leaching)
Through direct acid leaching experiments, it was found that maximum recovery of the manganese is less than 60% without any addition of a reductant. This is most likely due to the involvement of MnO 2 , which can only be effectively dissolved in sulfuric acid in a reducing atmosphere. In the second part of the leaching experiments, dextrin was added as the reductant. The amount of dextrin required for the complete reduction of manganese dioxide was calculated according to the reaction in Equation (5). Around 50% of the Mn present in the dust sample is soluble in acid without any reductant. Hence, the other half requires a reductant. Then, the stoichiometric need for dextrin was calculated as 0.05 g/g of dust (or 5% dextrin). However, for the initial studies, 50% excess or 0.08 g/g of dust (or 8% dextrin) was used to ensure sufficient dextrin presence. It should be noted that the reduction of MnO 2 by dextrin (or the oxidation of dextrin by MnO 2 ) is most likely not a single-step reaction. Previous studies showed that the acid leaching of the pyrolusite ore (MnO 2 ) in the presence of carbohydrates, such as glucose (C 6  dation products, such as HCOOH and HCHO [25][26][27]. Based on this information, it is very likely that the same is valid for the case of dextrin, another carbohydrate. 12MnO 2 + C 6 H 10 O 5 + 12H 2 SO 4 = 12MnSO 4 + 17H 2 O + 6CO 2 (5) Figure 5a shows the effect of the leaching temperature and acid concentration on Mn dissolution in the presence of dextrin. To ensure that the amount of acid is sufficient in the case of a possible complete Mn dissolution, these experiments were conducted at more than 12% acid concentration. The results show that, with an increase in the leaching temperature, Mn dissolution increases; however, the temperature effect is more prominent at higher acid concentrations. The manganese dissolution rate is the highest for all acid concentrations studied when the leaching temperature is increased to 90 • C. This is possibly due to the increase in the reaction rate between dextrin and MnO 2 Leaching efficiency also increases with increasing acid concentration. At low acid concentrations, this may be caused by the unavailability of the free acid that is consumed by both the direct and reductive leaching of manganese. With the addition of more acid, this problem should have been eliminated since, at 90 • C, the dissolution of Mn almost reaches completion with 20% acid concentration and is not affected by higher acid levels. Since acid concentrations of >20% will only consume high amounts of the neutralizing agent in the subsequent purification step, the optimum conditions for leaching become a 90 • C leaching temperature and a 20% acid concentration. Under these conditions, >95% of manganese can be dissolved into the solution.
rals 2021, 11, x FOR PEER REVIEW increases with increasing acid concentration. At low acid concentra caused by the unavailability of the free acid that is consumed by both ductive leaching of manganese. With the addition of more acid, this pro been eliminated since, at 90 °C, the dissolution of Mn almost reaches com acid concentration and is not affected by higher acid levels. Since acid >20% will only consume high amounts of the neutralizing agent in the cation step, the optimum conditions for leaching become a 90 °C lea and a 20% acid concentration. Under these conditions, >95% of mang solved into the solution.  To study the effect of leaching duration, sets of experiments were conducted at 70 and 90 • C with a 20% acid concentration and different time intervals. Leaching duration was varied from 15 min to 4 h, as shown in Figure 5b. With increasing leaching duration, Mn recovery drastically increases up to 1 h, and its effect becomes negligible with prolonged durations for both studied leaching temperatures. The time required for maximum Mn dissolution is higher for reductive leaching compared to direct leaching (i.e., with no reductant); this is due to the slower reaction between dextrin and MnO 2 . Lastly, to study the effect of the amount of reductant, experiments were conducted that varied the added dextrin amount at 90 • C for 1 h with a 20% acid concentration ( Figure 6). With an increase in the concentration of dextrin, manganese dissolution increases; this is due to the increased availability of dextrin for MnO 2 reduction. Maximum recovery of manganese (>95%) can be obtained with 8% dextrin addition (or 0.078 g/g dust). Hence, it is not possible to reduce the dextrin amount without losing Mn into the residue. Sulfuric acid leaching of the furnace dust without a reductant can dissolve of manganese into the solution. The optimum conditions for leaching without are a 30 °C leaching temperature, a 12% acid concentration, and a 30 min lea tion. Manganese dissolution can be improved through the addition of dextrin ant. Mn dissolution of >95% can be obtained at 90 °C with a 20% acid concentr leaching duration, and an 8% dextrin addition.

Electrolytic MnO2 (EMD) Production
After almost complete leaching of manganese from the furnace dust, the sulfate-rich solution can be used in the production of different end products. In the leachate was used in the production of electrolytic manganese dioxide (E ever, further studies can investigate the use of furnace dust for chemical mang ide (CMD) or manganese sulfate production. The latter is, for example, an source for the secondary battery industry. Figure 7a shows the effect of current density on current efficiency in a 0.2 containing electrolyte. The current efficiency (CE) of the process is calculate Equation (6) Sulfuric acid leaching of the furnace dust without a reductant can dissolve only <60% of manganese into the solution. The optimum conditions for leaching without a reductant are a 30 • C leaching temperature, a 12% acid concentration, and a 30 min leaching duration. Manganese dissolution can be improved through the addition of dextrin as a reductant. Mn dissolution of >95% can be obtained at 90 • C with a 20% acid concentration, a 1 h leaching duration, and an 8% dextrin addition.

Electrolytic MnO 2 (EMD) Production
After almost complete leaching of manganese from the furnace dust, the manganese sulfate-rich solution can be used in the production of different end products. In this study, the leachate was used in the production of electrolytic manganese dioxide (EMD). However, further studies can investigate the use of furnace dust for chemical manganese dioxide (CMD) or manganese sulfate production. The latter is, for example, an important source for the secondary battery industry. Figure 7a shows The EMD powder produced at 1 amp/dm 2 current density is shown in Figure 8b, the BSE image of the sample shows a rather smooth surface, with in the sample that developed during the mechanical removal of the deposit ode. The XRD pattern of the EMD powder is provided in Figure 9. It shows o of gamma-MnO2, which is suitable for battery applications. However, the measurement of the EMD powder is necessary in order to fully confirm this agreement with these results, the chemical analysis of the powder showed impurities were less than 0.1 wt.%.
Energy consumption (EC) during the process was calculated based on t Equation (7), where V, I, t, and W refer to voltage in volts, current in amperes in h, and the weight of the MnO2 deposited in kg, respectively. The energy the production of EMD powder was found to be in the range of 1.4-2.0 kWh produced. From Figure 7a it can be seen that current efficiency increases with an increase in the current density to some extent, and it decreases gradually thereafter. Maximum current efficiency was obtained at 1 amp/dm 2 , which is generally used in conventional EMD processes. At higher current densities, the rate of MnO 2 deposition is faster compared to the transport of ions. Moreover, the evolution of oxygen takes place at the anode due to the water-splitting reaction, which dominates over the MnO 2 deposition.
The addition of sulfuric acid to the electrolyte is required in order to improve the conductivity of the solution. Figure 7b shows the effect of the concentration of sulfuric acid on the current efficiency of the process. The efficiency is slightly increased by increasing the acid concentration from 0.05 to 0.25 M. This is due to the sufficient availability of the ions, which improves current conductivity. Above that value, there is no effect of the amount of acid on the current efficiency.
The EMD powder produced at 1 amp/dm 2 current density is shown in Figure 8a. In Figure 8b, the BSE image of the sample shows a rather smooth surface, with some cracks in the sample that developed during the mechanical removal of the deposit from the anode. The XRD pattern of the EMD powder is provided in Figure 9. It shows only the peaks of gamma-MnO 2 , which is suitable for battery applications. However, the bulk density measurement of the EMD powder is necessary in order to fully confirm this statement. In agreement with these results, the chemical analysis of the powder showed that all of the impurities were less than 0.1 wt.%.
Energy consumption (EC) during the process was calculated based on the formula in Equation (7), where V, I, t, and W refer to voltage in volts, current in amperes (amps), time in h, and the weight of the MnO 2 deposited in kg, respectively. The energy required for the production of EMD powder was found to be in the range of 1.4-2.0 kWh/kg of MnO 2 produced.
The overall flow sheet of the process is provided in Figure 10 with a partial mass balance. Based on 100 g of furnace dust input with 42.7% Mn, about 61 g of electrolytic MnO 2 can be produced, which corresponds to an overall Mn recovery rate of 90.3% from the dust sample.  The overall flow sheet of the process is provided in Figure 10 with a part balance. Based on 100 g of furnace dust input with 42.7% Mn, about 61 g of ele MnO2 can be produced, which corresponds to an overall Mn recovery rate of 90. the dust sample.  The overall flow sheet of the process is provided in Figure 10 with a partial mass balance. Based on 100 g of furnace dust input with 42.7% Mn, about 61 g of electrolytic MnO2 can be produced, which corresponds to an overall Mn recovery rate of 90.3% from the dust sample.

Conclusions
Ferromanganese furnace dust is an environmentally problematic by-pro FeMn alloy production. This study shows the feasibility of battery-grade ele MnO2 production from a real furnace dust sample. The main conclusions of the st

•
The particle size of the dust (D80) was 32 microns. The XRD result of the furn revealed that Mn3O4, MnO, and silica phases were present in the sample. Mn was 42.7%.

•
The leaching of the furnace dust without a reductant resulted in <60% Mn tion, with a 12% acid concentration, a 30 °C leaching temperature, and a 30 m ing duration. • Dextrin, a green, cheap, and water-soluble organic reductant, was found su a reductant.

Conclusions
Ferromanganese furnace dust is an environmentally problematic by-product of FeMn alloy production. This study shows the feasibility of battery-grade electrolytic MnO 2 production from a real furnace dust sample. The main conclusions of the study are:

•
The particle size of the dust (D 80 ) was 32 microns. The XRD result of the furnace dust revealed that Mn 3 O 4 , MnO, and silica phases were present in the sample. Mn content was 42.7%.

•
The leaching of the furnace dust without a reductant resulted in <60% Mn dissolution, with a 12% acid concentration, a 30 • C leaching temperature, and a 30 min leaching duration. • Dextrin, a green, cheap, and water-soluble organic reductant, was found suitable as a reductant. • 98.9% Mn dissolution is obtained by the optimum leaching conditions of a 90 • C leaching temperature, a 1 h leaching duration, a 20% acid concentration, and an 8% dextrin addition.

•
Optimized conditions for electrolytic manganese dioxide (EMD) production were: a current density of 1 amp/dm 2 and a sulfuric acid concentration of 0.25 M. The product obtained through the electrolysis process is a pure gamma MnO 2 phase. • A total manganese recovery of 90.3% from the furnace dust is possible with the proposed flow sheet. Funding: This research received no external funding.