Sensitivity analysis shows how much room for cost reduction there is by the improvement of individual parameters (Figure ), here investigated for the sorption capacity, the electrode thickness, the electrode density, and the activated carbon cost based on a cell design without carbon cloth as gas diffusion layer at a cost base of $115/ton as stated above. At a sorption capacity of 50, 100, 400, 600, 800, and 1000 mmol/kg, the cost changes to $459, $229, $57, $38, $29, and $23/ton, respectively. At an electrode thickness of 0.2, 0.4, 1.0, 1.3, 1.7, and 2.0 mm, the cost changes to $317, $176, $90, $77, $67, and $62. This is because the ratio the of adsorbing components (electrodes) relative to the non-adsorbing components (separator, carbon cement, current collector) increases with decreasing thickness. A change of electrode density to 0.05, 0.1, 0.3, 0.4, 0.6, and 0.8 g.cm -3 (at constant gravimetric sorption capacity), changes the cost to $359, $196, $88, $74, $60, and $53, respectively for the same reasons. Reduced activated carbon cost ($1.5/kg, $0.75/kg) changes the capture cost to $102, and $97/ton. Increasing the activated carbon cost to $6/kg, and $12/kg, increases the capture cost to $138, and $185/ton, respectively. It can be seen that the greatest sensitivity exists for the sorption capacity, and that a moderate further improvement to values of 600 mmol/kg can reduce the cost to < $50/ton (Figure ). The cost of sorbent is least sensitive to CO2 capture cost because the cost of the non-adsorbing components is higher. Increase of electrode density could be achieved by greater compression. A simple and effective way to reduce cost is to increase the thickness of the electrodes, as long as this can be done without significantly decreasing the adsorption rates, and increasing energy consumption due to increased resistance in the supercapacitor. The energy cost at an energy consumption of 179 kJ/mol is $56/ton at an electricity production cost of 5c/kWh (section S18). The contribution of energy cost would be reduced to $31 at 100 kJ/mol, and $16/ton at 50 kJ/mol, respectively. The cost may be further reduced by crushing electrode stacks at the end of their lifetime, and using them as soil conditioner, similar to biochar. Biochar is currently sold at a price of $2,500/ton indicating significant reductions in cost through the use of crushed, "spent" activated carbon electrode stacks as soil conditioner. Regeneration of the activated carbon is another potential way to reduce cost. The DOE 2025 cost target for post-combustion capture is $40/ton CO2. Although the above techno-economic analysis is not comprehensive, it indicates that the SSA has the potential to reach the DOE cost targets with moderate improvements. For example, the target would be met at a sorption capacity of 0.6 mol/kg, an electrode thickness of 1 mm, an electrode density of 0.4 g/cm , and an energy consumption of 50 kJ/mol without considering the end-of-lifetime value of the electrodes. The SSA technology does not only appeal for separation of CO2 from point sources (4-20% CO2) but also from air (0.04%) due to the combination of chemical robustness, moisture-compatibility, selectivity, reversibility, and low cost of materials. An investigation on the applicability of SSA to DAC is currently on the way in our laboratory.