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www.advancedsciencenews.com www.advancedscience.com ion removal because more ions can be transported through ion exchange membranes with the same energy consumption. As proven by ED research,[ 45 ] this approach can achieve low energy consumption for ion separation. Using an alternative membrane to AEM, which could facilitate ion diffusion from desalination to cathode compartment could also be a promising option to im- prove the desalination kinetics of SWB-D system. Since NASI- CON has been known as the resistance determining component in SWB-D system,[ 8 ] developing a highly conductive NASICON could lead to lower ohmic and diffusion resistance, thereby using a higher applied current would be possible. Note that the NASI- CON used in current SWB-D studies has a chemical composition of Na3 Zr2 Si2 PO12 .[ 8 ] For example, highly conductive NASICONs such as Na3.1 Si2.3 Zr1.55 P0.7 O11 [ 46 ] or Na3.4 Zr2 Si2.4 P0.6 O12 [ 47 ] could be suitable candidates (i.e., the resistance of ≈10−4 S cm−1 for Na3Zr2Si2PO12 and 5 × 10−3 S cm−1 for Na3.4Zr2Si2.4P0.6O12[47]) for SWB-D application. Another approach that can be considered to improve the desalination kinetics is the use of redox chemistry in cathode or catholyte as shown in the previous SWB study.[48] In this case, the sluggish kinetics of oxygen evolution and reduc- tion reactions can be replaced with relatively fast redox reactions, thereby improving the desalination kinetics of SWB-D systems. Designing a large-scale SWB-D cell with a minimized cost of cathodic C. C. would also be beneficial as the cathodic C. C. cost is ≈50% in SWBRect.. The anode compartment design will have a marginal impact on the overall material cost; however, it can render the system more compact, thereby minimizing the capital cost of any SWB based system including SWB-D system. Based on the aforementioned discussions, important con- cluding remarks can be made as follows: The material costs of AEM (50%) and separator (41%) are current hurdles for large-scale application of SWB-D. Energy recovery and cycling efficiency play crucial roles in determining the feasibility of SWB-D compared to other desalination technologies such as RO. When energy recovery of ≈96% and stable performance for 1000 cycles are achieved, an equipment cost of ≈1.02 $ m−3 can be expected, which is similar to RO (0.60–1.20 $ m−3). Flow-cell (or continuous system) development for SWB-D is urgently required for comprehensive comparisons. Continuous flow could facilitate ion diffusion across the AEM, which could re- move more ions without additional energy input. For SWB-D to compete with other seawater desalination processes, particularly RO, in addition to energy aspects, desalination kinetics must be significantly improved. For future studies, a more realistic cost analysis for large-scale SWB-D system can be done when material processing and casing costs are included. 4. Experimental Section Specific Energy Consumption: Whenever seawater is used for calcula- tion, the salt concentration was assumed as 0.6 m (≈35 g L−1 NaCl).[26] The salt removal of RO was assumed 100% because ≈99.7% of salt removal has been often reported.[ 49–51 ] For the calculation of the SEC of SWB-D, it was assumed that salt removal is proportional to energy consumption.[ 6 ] An energy consumption of 0.5 kWh m−3 was assumed for NF in SWB-D-NF at a feed concentration of 5200 ppm (when SWB-D removed 85% of salt from 35 000 ppm TDS). Moreover, a linear relation- ship between energy consumption and feed TDS in NF was used.[52] Note that the numbers used are an approximation and more research is needed to verify the maximum salt removal rate of SWB-D-NF using real seawater. This number Theoretical minimum energy required for seawater desali- nation was calculated by Gibbs free energy of separation at 50% of water recovery.[26,53] Detailed Information for Cost Calculations: The components used in calculations for SWBcoin were 0.8 g (NASICON), ≈2 cm2 (cathodic C. C.; carbon felt), 15 μL (anolyte; 1 m Biphenyl in diethylene glycol dimethyl ether), and ≈1.5 cm2 (anode; stainless steel mesh). For NASICON price, a mass-based element ratio was applied to each chemical needed to syn- thesize. Retail prices were used for the chemicals used during NASICON synthesis. The dimensions used in calculations for SWBRect. were 23.6 g (NASICON), 396 cm2 (cathodic C. C.; carbon felt), 6 mL (anolyte; 1 m Biphenyl in diethylene glycol dimethyl ether), and ≈68.3 cm2 (anode; stain- less steel mesh). For the material cost of SWB-D, which was calculated based on SWBcoin , an AEM area of ≈2 cm2 was considered. The AEM price was calculated based on the minimum unit price (200 $ m−1) multiplied by the area used (≈2 cm2 ).[ 54 ] For LIB calculations using retail prices, a coin cell (2325 coin cell; di- ameter ≈0.905 in; depth ≈0.098 in) with similar dimensions to SWB- coin was used. Accessible retail prices were used for the chemicals needed for the synthesis of each cell component. The cathode consists of LiNi0.6 Mn0.2 Co0.2 O2 (also known as NMC622), carbon black, polyvinyli- dene fluoride, and n-methyl-2-pyrrolidone (NMP). Aluminum foil was used as the cathodic C. C. and the electrolyte was a mixture of LiPF6, ethylene carbonate, and diethyl carbonate. Polyethylene membrane was used as the separator. The anode consisted of graphite, carboxymethyl cellulose and styrene-butadiene rubber, carbon black, and NMP. Acknowledgements This work was supported by the National Research Foundation of Korea (NRF) grant funded by the Korean government (MSIT) (grant number 2020R1A4A1019568). Conflict of Interest The authors declare no conflict of interest. Keywords cost analysis, desalination, energy storage systems, seawater batteries Received: March 29, 2021 Revised: May 27, 2021 Published online: [1] J. Schewe, J. Heinke, D. Gerten, I. Haddeland, N. W. Arnell, D. B. Clark, R. Dankers, S. Eisner, B. M. Fekete, F. J. Colón-González, S. N. Gosling, H. Kim, X. Liu, Y. Masaki, F. T. Portmann, Y. Satoh, T. Stacke, Q. Tang, Y. Wada, D. Wisser, T. Albrecht, K. Frieler, F. Piontek, L. Warszawski, P. Kabat, Proc. Natl. Acad. Sci. U. S. A. 2014, 111, 3245. [2] P. Rao, W. R. Morrow, A. Aghajanzadeh, P. Sheaffer, C. Dollinger, S. Brueske, J. Cresko, Desalination 2018, 445, 213. [3] J.Kim,K.Park,D.R.Yang,S.Hong,Appl.Energy2019,254,113652. [4] S. Lin, H. Zhao, L. Zhu, T. He, S. Chen, C. Gao, L. Zhang, Desalination 2021, 498, 114728. [5] Y. Zhang, S. T. Senthilkumar, J. Park, J. Park, Y. Kim, Batter. Supercaps 2018, 1, 6. [6] M.Ligaray,N.Kim,S.Park,J.-S.Park,J.Park,Y.Kim,K.H.Cho,Chem. Eng. J. 2020, 395, 125082. [7] N. Kim, J.-S. Park, A. M. Harzandi, K. Kishor, M. Ligaray, K. H. Cho, Y. Kim, Desalination 2020, 495, 114666. Adv. Sci. 2021, 2101289 2101289 (7 of 9) © 2021 The Authors. Advanced Science published by Wiley-VCH GmbHPDF Image | Seawater Desalination using Rechargeable Seawater Battery
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