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processes. In addition, the BPMED regeneration reaction can be driven electrically rather than using heat regeneration. As discussed later, the need for CO2 electrolyz- ers to operate using CO2 in the gas or liquid phase, as well as the heat resources available in the process, can further influence the technology utilized in the CO2 cap- ture step. While a reaction scheme and the specific technologies are proposed here in order to create a realistic air-to-barrel scenario, many possible alternate processes exist, and it might take some time before a final, preferred combination of technologies is real- ized. Nevertheless, the above exercise allows us to proceed with an analysis of the energy requirements and physical scales for each sub-process in a 10,000 ton/day plant. Energy Efficiency and Distribution of a Solar-Driven MeOH Synthesis Process To gain an understanding of the energy requirements, efficiency, and scale of such a proposed air-to-barrel system and the requirements of CO2 electrolyzers versus other sub-processes, we can take information known about each individual technol- ogy and combine them together to assess the entire system. The initial sub-process in the solar MeOH synthesis route (Figure 1) is the CO2 cap- ture reactor. Hollow fiber gas-liquid membrane contactors39 are well suited for the CO2 capture step, as these systems provide excellent contact between the aqueous capture solvent and the wind blowing through the reactor. Here, aqueous KOH is chosen as a capture medium given its integration with downstream CO2 conversion. Upon interaction with hydroxide, CO2 is fully converted to dissolved potassium car- bonate, capturing CO2 within a salt solution. For regeneration in the next sub-pro- cess, the capture solution is then pressurized to 50 bar using a pump. The capture process itself is estimated to require 13 kJ/mol CO2.40 From the capture unit, the CO2 is regenerated electrochemically in a BPMED step.38 Here, KOH can be regen- erated and recycled back to the capture step while a separate stream now containing dissolved CO2 in a pressurized water stream can be fed to the electrocatalytic system. This BPMED step requires a practical power input of approximately 215 kJ/mole CO2 (see Supplemental Information for details).41 The advantage of running electrodialysis at high pressures is that the CO2 produced essentially re- mains dissolved in water, which makes it an excellent feedstock for the subsequent CO2 electrolysis operation, avoiding the typical gas regeneration step that would otherwise require ~100 kJ/mol CO2. In addition, the CO2 in the pressurized aqueous stream can further be converted to pressurized CO, which is necessary for MeOH synthesis, which operates at 50 bar. Avoiding compression of both CO and H2 dur- ing production saves on the order of ~80 kJ/mol CO2 converted (see Figure 2 and Supplemental Information). Therefore, process integration with up and downstream systems, and the direct need for a high-pressure feedstock for MeOH synthesis can already give practical and minimum operating conditions for pressurized CO2 elec- trolysis, which deviate from most ambient-pressure academic studies.20,42,43 The electrochemical reduction of CO2 (Equation 3) then follows the electrodialysis step, producing CO as a product and O2 as a by-product of the anode reaction. As the solubility of CO in water is much less than that of CO2, this unit will produce pressurized gaseous CO, which is separated by phase, collected, and sent to the MeOH synthesis step. Pressurized CO2 reduction not only helps to increase current density but increased pressure aids the reaction in achieving near-unity selectivity.44 The solubility of CO2 in 1 M KHCO3 is 1.05 M at 25C and 50 bar, which ensures that CO2 will remain dissolved at the chosen concentrations for the electrolysis process. 1826 Joule 3, 1822–1834, August 21, 2019PDF Image | Pathways to Industrial Scale Fuel from CO2 Electrolysis
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