Since the reac on is mass-transport limited above 6.0V cell poten al, the first stages of the CSTR cascade would be run at 6.0 V to achieve the maximum possible rate at the minimum cell voltage. Ideally, the reac on should be con nued at this rate un l overreac on is problema c which would be informed by batch reac on profile analysis. For this reac on, overoxida on is apparent at above 72% conversion using 6.0 V cell poten al (Figure ). Hence, 72% becomes the target conversion at the highest voltage. Batch kine cs revealed that 72% conversion would require a residence me of 44 minutes at 6.0 V. To increase the overall throughput this reac on me was split between the first and second CSTR stages to give a residence of 22 minutes, resul ng in 36% conversion in each stage. For simplicity of design, residence me in all the reactors was uniform. Next, the last CSTR in the cascade was set at 3.5 V, again informed by batch kine cs showed low rates of overoxida on while maintaining a reasonable reac on rate (~10% conversion was expected with a residence me of 22 minutes). CSTR 3 was set at ~4.0 V to achieve the remaining 18% conversion in 22 minutes of residence me. An extended flow run to process 1kg of 1, using the cascading CSTR was setup to evaluate stability of the system. Prior to the flow run each cell was characterized by measuring the average resistance of the cell and the applied adjusted to compensate for the observed variability. The flow run ran for a total of 9.3 hours giving an overall yield of 85% of while overoxida on byproduct 3 was held below 2% as predicted from the design. Voltage, temperature, and conversion data were collected throughout the flow run to monitor the reac on progression and determine if the reactors had reached steady-state. A large amount of Ohmic hea ng was observed in CSTRs 1 and 2 which led to difficulty in controlling the reac on temperature to 15° C. This fluctua on led to elevated levels of 4 being formed in the early stages of the reac on. Future explora on of electrochemical reac ons at lower temperatures should examine the effect of Ohmic hea ng to accurately assess the amount of heat that should be removed from the system. However, outside of the temperature control challenges that were equipment based, the flow reac on performed admirably giving excellent steady-state performance. No electrode degrada on was detected, allowing us to comfortably extrapolate the throughput to 2.6 kg/day. With this lab scale reactor capable of producing kilograms of material per day, we turned our a en on toward developing a pla orm for scaling electrochemistry on a commercially relevant scale. Accordingly, a 10x scaleup reactor (based on electrode surface area, total volume was 6 L) was used to evaluate the feasibility of scaling a CSTR cascade for electrochemistry. A batch experiment was performed at 400 g scale at the same current density observed in the ini al stages as the small scale batch reac ons using 3.5 V applied poten al. This batch reac on achieved 95% conversion in 5.3h and gave 80% isolated yield of 2. At this scale, the amount of hydrogen gas generated by the reac on is an explosion hazard. To execute this scale-up safely, the reactor head was diluted with nitrogen gas to <1% hydrogen gas in the effluent gas (well below explosive levels). However, at scale the observed ini al current at the fixed poten al was only ~40% of what was expected from the same applied poten al on the smaller reactors. The difference in current is likely due to two factors. The first is the difference in electrode surface area to volume of reac on which was ~33% on scale. The second was difference in electrode spa al arrangement. Both of these varia ons between scales evolved in itera ons of the large scale reactor, where the volume was decreased to make use of a standard length of material (12" rods) and to have the electrodes arrays so that current could be supplied through a single parallel manifold. The results of the ini al scale-up experiment highlight the challenges in electrochemistry where small changes in configura on of the electrodes can lead to inconsistent results between scales, requiring calibra on of the reactors under standard condi ons. To facilitate future scale-up efforts, the smaller scale reactors will be redesigned to represent the large scale reactor configura on. The reac on was re-evaluated with a higher applied poten al (5.2V) in a 700 g batch (83% isolated yield) which gave the expected rate and reac on profile to results seen at lower poten al at smaller scale. Extrapola ng these results shows that this reactor design is capable of >30 kg/day throughput if a 4-CSTR cascade was applied. In conclusion, we have demonstrated a 1 kg flow reac on (2.6 kg/day) using a novel CSTR cascade for constant poten al electrochemical reac ons. Evalua ng the cri cal reac on parameters provided a balance between achieving high throughput in a small footprint reactor, while maintaining high selec vity was cri cal to the success of the CSTR cascade design. This design allows for a greater degree of modularity compared to exis ng solu ons, with access to a wide array of commercially available electrode materials which can easily be subs tuted into the reactor. Avoiding complex reactor design will greatly reduce the barrier to implemen ng electrochemical reac ons on scale as it provides a clear path from screening reac ons using HTE to scale-up. Future efforts will focus on improving mass transport through the use of improved impellor geometry to further increase the throughput that can be achieved using this design.