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Electrochemical reduction of different Ag(i)-containing solutions in bioelectrochemical systems for recovery of silver and simultaneous power generation

In this study, dual-chamber bioelectrochemical reactors (i.e., R1, R2, R3, and R4) were employed to investigate the Ag recovery and electricity production from different Ag(i)-containing artificial wastewaters (i.e., Ag+ solution, [Ag(NH3)2]+ and [Ag(S2O3)2]3− complexes, and mixed metal solution). Results showed that the electrochemical reductions of Ag(i) ions in all reactors were rapid reactions. The reaction rate in R1 was the fastest. At the same initial conditions (i.e. Ag(i) concentration of 1000–1080 mg L−1), the Ag recovery efficiency was 81.8% for R3 operated with the [Ag(S2O3)2]3− complex. Although high Ag removal efficiency (i.e., >99%) was found in other reactors, some diffusion of positively charged Ag(i) ions through the membrane was also observed along with the electrochemical reduction. In all cases, pure silver electrodeposits, mainly as dendrites and crystals in different morphologies, were observed at the cathode surfaces when characterized by SEM, EDX, and XRD. The performance of electricity production was evaluated by the open circuit voltage (OCV) and maximum power density (Pmax) obtained during the BES operation. Reactor R1 showed better performance (i.e., OCV of 828 mV, Pmax of 8258 mW m−3), due to its high standard reduction potential. The lower performance in other reactors was due to the complexity of solutions, other co-existing metals (mixed metal solution), and lower standard reduction potential. In general, the existing forms of Ag(i) in solutions affect the Ag(i) reduction rate. This further influences the Ag removal efficiency, morphology of electrodeposits, and power generation.


Introduction
A variety of methods have been studied for the recovery of metals (for instance, silver) from aqueous solutions and wastes. [1][2][3][4] There has been much effort to develop recovery techniques that are cost-effective and sustainable. In recent times, technologies based on microbe-metal interactions, such as bio-sorption, bioremediation, and bio-reduction, have received much attention as biotechnological metal-recovery processes. 5 Microbe-based technology is a cost-effective choice for concentrating diffuse metallic ions from effluents for recovery. However, many difficulties still exist with this method, which limit the practical applicability. Toxicity to microorganisms due to the complex physicochemical conditions of waste streams (e.g., too low or too high pH, high metal concentration, other co-existing recalcitrant compounds) is a major concern. In addition, the biomass aer recovery needs to be rened and post-treated by further processes that lead to extra costs, to obtain a recoverable product (pure metals). Thus, other biobased recovery techniques need to be explored to solve these issues.
Recently, bio-electrochemical systems (BESs) have been shown as a platform technology for integrated waste treatment along with energy and resource recovery. [6][7][8] A typical BES consists of an anode and a cathode chamber, separated by an ion exchange membrane (IEM). However, BESs differ in conguration, which depends on the target functions to be accomplished. In the anode chamber, biodegradable substrates, such as organic matter, are oxidized by microorganisms via anaerobic metabolism to harvest electrons. These electrons are then transferred to the anode electrode through different extracellular electron transfer (EET) mechanisms. The electron ow is then directly captured through an electrical circuit and is delivered to the cathode for either electricity production, hydrogen generation, or removal of recalcitrant contaminants. 8 In principle, any compound with a high redox potential can serve as the catholyte to accept the electrons. 9 Metal ions, therefore, can be utilized as terminal electron acceptors (TEAs) to be reduced, forming metallic electrodeposits on the cathode surface. Based on the BES mechanism, organic-rich wastewater and metal-laden solution are fed separately into the anode and cathode chamber, respectively, where the biological oxidation and electrochemical reduction occur simultaneously. Thus, a BES reactor, which can be considered as a fuel cell, serves the functions of a biological wastewater treatment system and a bio-method for the recovery of metals from aqueous solutions. Fundamental mechanisms and engineering feasibilities of BES technology for the removal and recovery of different metals have been reviewed by some researchers, indicating BES as a promising approach. [9][10][11] Due to the valuable features and widespread use of silver in many industrial applications, the recovery of this precious metal from effluents has been emphasized in industrial waste management and treatment. The components of waste are relatively complex, where a variety of organic and inorganic substances (e.g., ammonia, EDTA, and thiosulfate) usually exists. [12][13][14] Thus, the effluents normally contain Ag at high concentration, in which Ag ions exist in the form of either simple silver salts (e.g., silver nitrate AgNO 3 ) or complexes (e.g., [5][6][7][8][9][10][11][12][13][14][15] or silver(I) diammine [Ag(NH 3 ) 2 ] + (ref. 13)). Since 2012, a few BES studies of silver recovery coupled with power generation have been conducted, in which the effects of operational parameters (e.g., pH, initial Ag(I) concentration) were investigated. [16][17][18][19][20] The inuence of different IEMs on BES performance has also been examined, recently. 21 However, so far there has been no study that compares the BES performance among different Ag(I)-containing solutions. Different existing forms of Ag(I) that are used as catholytes correspond to different standard redox potentials (E 0 ca ). These redox potentials have a distinct inuence on Ag(I) reduction and further affect the recovery efficiency. This is because E 0 ca is directly related to the working cathodic potential (E ca ), a decisive factor in the kinetics of electrochemical reactions. In addition, BES performance is also characterized by the formation, growth, and chemical composition of silver deposits that are formed on the cathode surface. These silver deposits are affected by the types of Ag(I) solutions used during BES operation. The main structure of silver atoms is crystalline (i.e., facedcentered cubic silver), which needs to be obtained when recovering silver from aqueous solution. Thus, a comparison of BES performance for different types of Ag(I) solutions is required to understand the reductive capacity of Ag(I) ions serving as TEAs in the cathode chamber.
In this study, four independent BES reactors are employed to investigate the silver recovery and simultaneous electricity production from articial Ag(I) solutions. These solutions are simulated based on the predominant Ag(I) forms in real industrial effluents (i.e., silver electroplating, photographic processing). They are (i) Ag + solution from AgNO 3 , (ii) [Ag(NH 3 ) 2 ] + complex, (iii) [Ag(S 2 O 3 ) 2 ] 3À complex, and (iv) multimetal solution containing Ag + , Fe 3+ and Cu 2+ as nitrate forms.
All reactors are operated at the same initial conditions, and the kinetics of the reactions is analysed to compare the Ag(I) reduction rate and removal efficiency. The morphology and composition of the deposits on the cathode surfaces are also analysed to conrm the silver electrodeposits and show the differences in the morphology due to the different types of Ag(I) solution. The electricity production in all cases is performed through the electrochemical parameters measured from polarization tests. These actual electrochemical parameters are then compared with theoretical thermodynamic values to show the differences in performance. The overall goal is to highlight the role of TEAs in the cathode chamber, as Ag(I) ions exist in different forms, and clarify their effects on BES performance. The ndings from this work will be useful for further BES studies to investigate the recovery of silver from real Ag(I)-containing wastewaters.

Fabrication and installation of BES reactors
Four similar cube-shaped BES reactors, made from acrylic plates, are designated reactors R1, R2, R3, R4, corresponding to four different types of Ag(I) solution. Each reactor consisted of an anode and a cathode chamber (i.e., 12 cm long Â 6 cm width Â 22 cm high, with a working volume of 1.0 L for each chamber) separated by a cation exchange membrane CMI-7000S (Membrane International, Inc. USA). The membrane, with a surface area of 264 cm 2 , was pre-treated by immersion in 5% NaCl solution for 12 hours to allow for hydration and expansion. Carbon brush (15 cm Â 6 cm), prepared by twisting carbon ber (Thai Carbonber Co., Thailand) with a Ti wire of 1.0 mm in diameter (Prolog Titanium Co., Ltd), served as the anode. The cathode was a graphite plate (90 cm 2 , Fujian, China). Before making electrical connections with the Ti wire, both electrodes were pre-treated to eliminate contaminants and enhance conductivity.
The carbon brush was rst cleaned by soaking in pure acetone (overnight). Aer that, it was treated with acid by soaking in a mixture of ammonium peroxydisulfate (200 g L À1 ) and concentrated sulfuric acid (100 mL L À1 ) for 15 min. The anode was then heat-treated in a muffle furnace at 450 C for 30 min and washed three times with distilled water. According to previous studies, the above procedure increased power generation by 25% due to an increase in the specic area, which facilitated bacterial adhesion and enhanced the charge transfer from the bacteria to the electrode. [22][23][24] The graphite plate cathode was immersed for more than 24 h in 2 mM potassium permanganate solution (KMnO 4 ) and washed thoroughly with distilled water before assembling. All reactors were then connected to a computer equipped with a data logger (Grant Instruments, Cambridge Co., Ltd), to record cell voltage production during experiments (Fig. 1).

Inoculation and acclimatization
Mixed-culture inoculum, anaerobic sludge (0.1 L) collected from the digester of a brewery wastewater treatment plant (Pathum Thani, Thailand), was used to activate the biological activities in the anode chambers of all reactors. Compared to pure cultures, the higher diversity of microbial communities in mixed cultures can make bio-electrochemical processes more stable and efficient due to their higher adaptability, stability, and productivity. 25,26 The anolyte (900 mL), supplied as a nutrient source for the microbial growth, includes (per liter) CH 3 COONa (1.28 g) as the substrate, Na 2 HPO 4 (3.55 g), KH 2 PO 4 (3.4 g), NH 4 Cl (0.31 g), and yeast extract (0.2 g). The initial organic loading of the anolyte, as represented by COD concentration, was 1000 mg L À1 . It was reported that acetate is a simplest substance that has been extensively used as a carbon source, to induce electrochemical active bacteria (EAB). 27 Preliminary results showed that a BES reactor inoculated with acetate provided a faster rate of cell voltage response during the inoculation stage, as compared to glucose. 19 The cathode chamber was lled with buffer solution (1.0 L), containing (per liter) NaH 2 PO 4 $2H 2 O (4.77 g), Na 2 HPO 4 (2.75 g), and NaCl (2.93 g). During the inoculation stage, the anode chamber was kept in anaerobic conditions to proceed with the bio-anodic reactions, in which CH 3 COONa acted as an electron donor. In contrast, the cathode chamber was purged continuously with air (80 mL min À1 ), to supply oxygen (O 2 ) as an electron acceptor. An electrical circuit made of Ti wire with a 1000 U resistor was connected for the electron ow from the anode to the cathode. The system worked as a fuel cell, in which the production of cell voltage (E cell ) was monitored and recorded by a data logger that was connected to a PC (Fig. 1).
The inoculation of all reactors was conducted under batchfed conditions and room temperature (20-25 C). The anolytes and catholytes were refreshed at the end of each cycle (i.e., 5-6 days), when the E cell dropped sharply due to a shortage of substrate in the anode chambers. The system was considered to be successfully acclimated when a stable and repeatable E cell (i.e., 300-350 mV) was obtained aer 6 feeding cycles (5-6 days/ each cycle). The airow was then stopped in the cathode chamber, and BES operation was started simultaneously in all reactors for silver recovery and electricity production.

BES operation for silver recovery and power generation
The BES operation was designed for a batch-feeding mode in 48 hour experiments, in which the anolytes were refreshed to keep the initial organic loading (i.e., COD 1000 mg L À1 ) similar in all reactors. The catholyte in each reactor was replaced by the corresponding Ag(I) solution, which served as an electron acceptor at this stage. Specically, Ag + solution (1000 mg Ag + per L), [Ag(NH 3 ) 2 ] + complex (1000 mg Ag(I) per L), [Ag(S 2 O 3 ) 2 ] 3À complex (1080 mg Ag(I) per L), and mixed multi-metal solution (1080 mg Ag + per L, 1120 mg Fe 3+ per L, and 64 mg Cu 2+ per L) were fed into the cathode chambers of reactors R1, R2, R3, and R4, respectively. The catholytes were prepared as follows: -For Ag + and mixed multi-metal solutions: soluble nitrate salts (i.e., AgNO 3 , Fe(NO 3 ) 3 , Cu(NO 3 ) 2 ) were dissolved in deionized (DI) water. The original pH of the Ag + solution was adjusted to 2.0 by adding HNO 3 acid, while the original mixed solution, as measured, was 2.2.
-For [Ag(S 2 O 3 ) 2 ] 3À complex: AgBr was dissolved in excess 100 mM Na 2 S 2 O 3 solution. The AgBr was produced by mixing 10 mM AgNO 3 (corresponding to 1080 mg Ag/L) with 10 mM KBr. The excess Na 2 S 2 O 3 solution prevents the formation of the sparingly-soluble silver(I) thiosulfate precipitate Na[Ag( The soluble complex of [Ag(S 2 O 3 ) 2 ] 3À can be formed which is theoretically the most stable since it has the lowest Gibbs free energy of formation. 28 The original pH of the [Ag(S 2 O 3 ) 2 ] 3À complex was 7.39 and was not adjusted during the operation.
-For [Ag(NH 3 ) 2 ] + complex: Ag 2 SO 4 (Ag + concentration of 1000 mg L À1 ) was dissolved in an excess amount of 30% NH 4 OH solution and de-ionized (DI) water. The mixture was heated gently on a hotplate with occasional stirring until the solid Ag 2 SO 4 dissolved completely. Silver existed in the form of [Ag(NH 3 ) 2 ] + complex. The original catholyte pH was about 10.2 and was not adjusted during the operation.
The anode and cathode chambers were purged with N 2 gas (80 mL min À1 ) for 15 min to eliminate the dissolved oxygen. The whole system was then kept in anaerobic conditions by sealing with gas-tight septa during the operation. An external resistance (R ext ) of 5 U was connected to the electrical circuit to maximize the current transferred from the anode to the cathode (Fig. 1).
During the operation for silver recovery and electricity production, acetate (CH 3 COO À ) ions served as electron donors in the anode chamber, whereas Ag(I) ions in different forms replaced O 2 to act as electron acceptors in the cathode chamber. The anodic and cathodic reactions are hypothesized as follows: The ideal biological reaction of the electron donors in the anode chambers of all reactors is: 29 In contrast, the possible reactions of electron acceptors in the cathode chamber of each reactor are shown in the following equations: 30 Reactor R4: Ag (aq) + + e À / Ag 0 (s) , E 0 ca1 ¼ +0.799 V (vs. SHE)(5a) The given hypothesis is that all reactions occur spontaneously and dominantly, except for reactor R4. In reactor R4, the cathodic reactions, shown in eqn (5b) and (5c2), are not energetically favourable. Accordingly, pure silver was expected to be recovered as metallic deposits on the cathode surface, accompanied by power generation as a by-product in all BES reactors.
Polarization curve analysis was also conducted in all BES reactors to characterize them as microbial fuel cell (MFC) systems. The analysis started when the reactors were operated for 10 hours. The reactors were rst kept in open circuit to obtain the stable open circuit voltage (OCV), and the R ext was then varied gradually from 10 000 U to 5 U. The E cell was observed at about 15 minutes, and the temporarily stable values were recorded to avoid changes in the substrate/product during the measurement. The current density (I) and power density (P) were then calculated, based on the stable E cell obtained at each R ext .
All chemicals used in this study are analytical grade and obtained from Fisher Chemical (Thermo Fisher Scientic, Belgium and Fisher Scientic, UK), Ajax Finechem Pty Ltd, Merck Millipore (Darmstadt, Germany), and Laboratory Reagents and Fine Chemicals (Loba Chemie Pvt. Ltd, India). The solutions and reagents were prepared by using DI water.

Analytical methods and calculation
The anolytes and catholytes in all reactors were sampled every 4 hours to determine the remaining COD and Ag(I) concentration. Before analysis, all samples were ltered through syringe lters (NY 0.45 mm (Allpure)) to eliminate particles or suspended biomass, which may come out when sampling. The Ag(I) concentration in the catholytes was measured by an Inductively Coupled Plasma (ICP) Spectrometer (Optima 8000, Perki-nElmer, USA). Soluble COD measurement was based on the Closed Reux, Titrimetric method. 31 All measurements were performed in duplicate and the results reported are the average values.
The decrement of COD concentration (DC s , mg L À1 ) at time t was calculated as The silver removal efficiency (RE%) at time t was calculated as For electrical performance, the E cell (mV) production was monitored with a data logger (Grant Instruments, Cambridge Co., Ltd) every 10 min during the operation and analyzed by using Squirrel View soware 2010. The power density, P (mW m À3 ), and coulombic efficiency, CE (%), were calculated as follows: In the above equations, COD 0 is the initial COD of anolyte fed into the anode chamber (1000 mg L À1 ). COD t is the COD at time t (mg L À1 ). C 0 is the initial Ag(I) concentration in the catholyte (mg L À1 ), and C t is the remaining Ag(I) concentration in the catholyte at time t (mg L À1 ). R ext is the external resistance installed in the system. R ext was xed at (i) 1000 U during the inoculation stage, (ii) 5 U during operation, and was varied from 10 000 to 5 U during polarization curve analysis. I (mA) is the current calculated by E cell /R ext . Then, the current density was obtained as E cell /(R ext Â V). V is the working volume of the anode chamber (1.0 L), and F is the Faraday constant (96 485 C mol À1 e À ).
Aer 2 months of BES inoculation and operation, all reactors were emptied. The graphite plate cathodes were taken out of the reactors and air-dried at room temperature. Deposits covering the cathode surfaces were scraped to characterize the morphology and chemical composition by a scanning electron microscope (SEM) (SU8030 or S-3400N, Hitachi, USA and JSM-7800F, JEOL, USA), equipped with an energy dispersive X-ray (EDX) detector (Metek, Apollo XP 2060, USA and X-Max N , Oxford Instruments, UK).

Kinetic analysis of Ag(I) reduction and Ag removal efficiency
Four BES reactors (i.e., R1, R2, R3, and R4) were operated at the same conditions (i.e., initial COD loading of 1000 mg L À1 , initial Ag(I) concentration of 1000-1080 mg L À1 ). The decrease of Ag(I) concentration in the catholytes of each reactor during operation is shown in Fig. 2. The remaining Ag(I) concentration in the catholytes of R1, R2, R3, and R4 aer 48 hours of operation was 3.45, 3.28, 197.25, and 3.15 mg L À1 , respectively. The Ag(I) reduction trends in reactors R1, R2, and R4 were similar (Fig. 2), whereas a slightly sloped curve of Ag(I) reduction was found in reactor R3. This may be due to the existing form of Ag(I) in R3 (i.e., a negatively charged complex), as compared to the common forms used in the other reactors (i.e., positively charged free ions or complexes). The charge state of Ag(I) in the catholyte is also an important factor, as it inuences the migration of ions between the two chambers to maintain the electroneutrality. This inuences the reduction rate of the anodic and cathodic reactions. Thus, high Ag removal efficiency (RE) (over 99%) was found for R1, R2, and R4, whereas a lower RE of 81.8% was obtained in R3 (Table 1). This can be explained by the low standard reduction potential of [Ag(S 2 O 3 ) 2 ] 3À complex in R3 (i.e., E 0 ([Ag(S 2 O 3 ) 2 ] 3À /Ag 0 ) ¼ + 0.016 V vs. SHE), as compared to that of Ag + in R1 and R4 (i.e., E 0 (Ag + /Ag 0 ) ¼ + 0.799 V vs. SHE) and [Ag(NH 3 ) 2 ] + in R2 (i.e., E 0 (Ag(NH 3 ) 2 + /Ag 0 ) ¼ + 0.373 V vs. SHE) (eqn (2)-(5a)). Basically, the reduction potential of cathodic electron acceptors (E ca ) directly affects the thermodynamic cell voltage and inuences the actual E cell production, which plays an important role in the reduction rate. A decrease of Ag(I) concentration was hypothesized due to the electrochemical reduction of Ag(I) ions by accepting electrons transferred from the anode, as shown in eqn (2)-(5a). To compare the Ag(I) removal rate among the 4 reactors, the kinetic reactions of Ag(I) reduction in the system were analyzed. Results showed that the reduction followed and matched the rst-order reaction (i.e., C t ¼ C 0 e Àkt ), where k is the reaction constant (h À1 ) ( Table 1). The reduction rate of Ag + ions in reactor R1 was faster than that of the other reactors, as the reaction constant k was calculated to be 0.155, 0.117, 0.041, and 0.129 (h À1 ) in reactors R1, R2, R3, and R4, respectively. The linear regression coefficient R 2 was >0.95 in all cases (Table 1). This result indicated that the removal rate of Ag + ion was more rapid than that of Ag(I) complexes. This nding is in line with that found by Tao, et al., 18 in which the reduction of Ag + ion was more favorable and rapid than the [Ag(S 2 O 3 )] À complex.
However, the catholyte pH was adjusted in reactors R1 and R4 to maintain the acidity (i.e., pH of 2.0) to keep silver in a dissolved state (existing as Ag + ions), which results in a high cost of operation. Furthermore, Ag loss due to the diffusion of positively charged Ag(I) ions from the cathode chamber to the anode chamber through the CMI-7000S membrane was found in reactors R1, R2, and R4 during the experiments and is reported in previous publications. 20,21 Although a fast decrease of Ag(I) concentration and high Ag removal efficiency (i.e., >99%) were obtained with reactors R1, R2, and R4, it was ascribed to the electrochemical reduction of Ag(I) to form the recovered product as Ag 0 deposits on the cathode surface and by the precipitation on the membrane surface and diffusion to the anode chamber. In reactor R3, [Ag(S 2 O 3 ) 2 ] 3À complex was reduced spontaneously only through the electrochemical reaction in the cathode chamber without diffusion or loss of silver. Thus, the Ag removal efficiency as shown in Table 1 (i.e., 81.8%) could be interpreted as Ag recovery efficiency. Since [Ag(S 2 O 3 ) 2 ] 3À complex is a typical and commonly existing form of silver in real wastewater, it is believed that BES technology is feasible for practical situations.

Performance in electricity production
The effects of Ag(I) forms on power generation are evaluated by considering the electrochemical parameters obtained from the polarization curve test. In this analysis, the external load of the electrical circuit in four reactors was changed by decreasing periodically the R ext from 10 000 U to 5 U. The temporarily stable cell voltages (E stable cell ) were recorded at pseudo-steady state. The current density (I) and power density (P) were then calculated using Ohm's law. Polarization curves (E1-E4) represented E stable cell as a function of I (Fig. 3a), while power curves (P1-P4) described P as a function of I (Fig. 3b).
In Fig. 3a, when the highest R ext is applied (i.e., 10 000 U), corresponding to the lowest I produced (i.e., $0 mA m À3 ), the measured E stable cell is dened as the open circuit voltage (OCV). The OCV is normally used to evaluate the actual performance of a fuel cell. Fig. 3a shows that there was a signicant difference in OCV values among the four reactors. The highest OCV of 828 mV was found in reactor R1, where Ag + solution served as the catholyte. In reactor R4, although a Ag + salt was used, OCV decreased dramatically to 645 mV due to the effects of other metallic salts that co-exist in the catholyte (i.e., Cu 2+ and Fe 3+ ). When Ag(I) complexes ([Ag(NH 3 ) 2 ] + and [Ag(S 2 O 3 ) 2 ] 3À ) were investigated in reactors R2 and R3, lower OCVs (i.e., 445 and 241 mV, respectively) were found. These results conrm the  impacts of the theoretical cathodic reduction potential (i.e., E ca ) on the thermodynamic cell voltage (i.e., E therm ¼ E ca À E an ), which directly inuences the actual value (i.e., OCV). When different Ag(I) solutions were examined, the higher the E ca produced by the Ag(I) solution, the higher the OCV obtained in the system. A comparison of the electrochemical values Paper (calculated theoretically, i.e., E ca and E therm ) and the actual performance (i.e., OCV) obtained in each reactor, corresponding to a specic Ag(I) solution, is summarized in Fig. 3c. In terms of power curves (Fig. 3b), the maximum power density (P max ) as the peak of the P curve was highest for reactor R1 (i.e., P max of 8258 mW m À3 ), as compared to R2 (i.e., P max of 1147 mW m À3 ), R3 (i.e., P max of 1500 mW m À3 ), and R4 (i.e., P max of 2472 mW m À3 ) (Fig. 3c). This shows that the cathodic reduction of Ag + ions in a BES reactor is energetically more favorable than other Ag(I) complexes and the mixed solution, which was due to the higher E ca of the catholyte, leading to a higher cell voltage and power density. Although the actual OCV obtained in reactor R 2 with [Ag(NH 3 ) 2 ] + complex (445 mV) was higher than that in reactor R3 with [Ag(S 2 O 3 ) 2 ] 3À complex (241 mV), P max2 was lower (1147 mW m À3 ), as compared to P max3 (1500 mW m À3 ). This may be due to the effects of internal resistance (R int ) resulted from the resistance of the electrolyte and membrane in the system. In BES studies, it was reported that linear polarization curves (E) are most oen encountered. The R int , in which the ohmic resistance (R U ) is dominant, can be determined from the slope of E curves. 29 In this study, the slope of E2 (as shown in Fig. 3a) is sharper than that of E3, indicating a higher R int in reactor R2. This result was explained by the effects of fouling at the surface of the CMI-7000S membrane. This fouling was due to the formation of inorganic precipitates and the diffusion of positively charged [Ag(NH 3 ) 2 ] + complex in reactor R2, causing higher R int of the membrane and lower performance in electricity production. 20 Generally, the reactor congurations and electrode materials inuence the BES performance due to their effects on internal resistance and cell voltage production. Thus, in order to enhance the performance of electricity production, electrode material that have high redox activity and low-cost are more attractive. For example, ultrathin Ni(OH) 2 nanosheets assembled into three-dimensional (3D) interspersed ower-like nickel hydroxide provided a large contact area with the electrolyte, reduced the polarization of the electrochemical reaction, and provided more active sites, which yielded a high capacitance and improved the electrochemical performance. 32 Characterization of electrodeposits at the cathode surfaces Prior to use, the graphite plate cathodes in the four reactors are the color of black-carbon. Aer 2 months of inoculation and operation, bright deposits were observed on the cathode surfaces in all cases. To conrm the successful BES operation for the recovery of silver, these deposits were scraped from the cathode and characterized by SEM, EDX, and XRD.
In SEM analysis, different morphologies of the cathodic deposits were found. Specically, deposits with polyhedral and small dendritic structures were detected on the cathode of R1 operated with AgNO 3 solution (Fig. 4b). This polyhedral form was comparable to the crystal structure of silver atoms (i.e., faced-centered cubic silver). For R2 operated with [Ag(NH 3 ) 2 ] + , larger dendritic structures were found (Fig. 4c). These dendrites have long trunks and short branches which look like a shbone. A similar dendritic crystal structure was also detected in the cathode surface of R4 when a mixed solution containing Ag + was used (Fig. 4e). For the [Ag(S 2 O 3 ) 2 ] 3À complex, different-sized clusters of deposits were observed on the cathode surface of R3 ( Fig. 4d). This morphology of deposits on R3 was different from the others, where incoherent crystal particles or dendrites were normally formed. The morphology of cathodic deposits in the four reactors was affected by the E cell output, which is related to the intensity of electron ow for the reduction of Ag(I) in the catholyte, as shown in eqn (2)- (5). It was reported that in an electrochemical reaction, the current density is related to the reaction rate and inuences the nucleation and growth of silver particles, as shown in Fig. 4a (i.e., from polyhedral aggregates to long thick rods, followed by thick dendritic structures, and a mixture of dendrites and small cubic particles). 33 The SEM results were veried by EDX (Fig. 5), in which sharp peaks at an energy level of 2.98 keV were found in all cases, indicating the deposits were comprised of pure silver. The XRD shown in Fig. S1 † (Appendix) also conrmed the EDX results. The XRD results matched the standard patterns of silver (i.e., JCPDS card no. 04-0783). All peaks can be indexed to facecentered-cubic silver, where the diffraction peaks occur at 2q values of about 38 , 44 , 64 , 77 , and 81 , corresponding to the reection of (111), (200), (220), (311), and (222) planes, respectively. No peaks from other phases (e.g., S-related compounds as Ag 2 S and Ag 2 SO 3 ) were detected. This indicated high-purity electrodeposits of silver achieved in this study.

Conclusions
This study found that different types of Ag(I)-containing solutions (i.e., Ag + solution, [Ag(NH 3 ) 2 ] + , [Ag(S 2 O 3 ) 2 ] 3À complex, and mixed multi-metal solution containing Ag + , Fe 3+ , Cu 2+ ) employed in BES reactors resulted in different performance for Ag recovery and simultaneous electricity production. In all four reactors, Ag(I) was reduced electrochemically to form deposits on the cathode surface. The highest reduction rate (i.e., kinetic reaction constant, k of 1.55 h À1 ) was found with Ag + solution, as compared to the other Ag(I) solutions (i.e., [Ag(NH 3 ) 2 ] + complex, k of 0.117 h À1 ; [Ag(S 2 O 3 ) 2 ] 3À complex, k of 0.041 h À1 ; and mixed multi-metal solution, k of 0.129 h À1 ). Aer BES operation in independent reactors (i.e., 48 hours for each batch of experiments), a recovery efficiency (RE) of 81.8% was obtained with [Ag(S 2 O 3 ) 2 ] 3À complex. High removal efficiencies (i.e., >99%) were found for Ag + , [Ag(NH 3 ) 2 ] + , and the mixed multi-metal solution. This resulted from either cathodic electrochemical reaction or diffusion of positively charged Ag(I) forms through the CMI-7000S membrane, which may cause Ag loss in the system. Different morphologies of electrodeposits formed at the cathode surfaces were found with SEM-EDX-XRD characterization, in which dendrites and crystals were the main structures. In terms of electricity production, Ag + solution showed the best performance with the highest P max (i.e., 8258 mW m À3 ) and OCV (i.e., 828 mV), which was due to its high standard reduction potential.

Conflicts of interest
There are no conicts to declare.