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for extraction is 0.004 moles/min (0.0023 moles/L CO2 (100 mg/L) x 1.89 L/min). The RO flow rate to the electrode compartments is 0.06 gal/min (230 mL/min). Table 2. E-CEM Operating Configuration CO2 Concentration Extracted at 100% efficiency (eq 13) CO2 Concentration Extracted at 92% efficiency (eq 13) H2 Concentration Extracted at 100% (eq 14) 0.0040 moles/min 0.0037 moles/min 0.002 moles/min 0.0040 moles/min 0.0037 moles/min 0.010 moles/min Applied Current to Electrochemical Cell 7 amps 30 amps Operating Seawater Flow Rate Center Compartment 0.5 gal/min 0.5 gal/min Operating RO Flow rate to Electrode Compartments 0.06 gal/min 0.06 gal/min Calculated Synthetic Fuel for 100% CO2 and H2 0.027 gal/day In these test series a 30 volt, 30 amp DC power supply is used to provide current to the acidification cell. Table 2 provides the operating flow rates and currents that were evaluated in the different test series and the calculated minimum amounts of CO2 and H2 extractable at those currents and process efficiencies of 92% and 100%. The Table shows that the maximum calculated extractable CO2 when the module is operating at 92% efficiency and 7 amps is 0.0037 moles/min. Thus the theoretical flow rate in mL/min to current ratio is estimated to be 270 mL/amp (equation 13). The available hydrogen at 7 amps is 0.002 moles/min. At these hydrogen concentrations, a mole ratio of 0.5:1 H2 to CO2 is inefficient for hydrocarbon production. The module was operated during these evaluations over a range of current density to establish relationships for module performance using KW-city water as the electrode source. There are two principle reactions that take place in the synthesis of a jet fuel fraction (C11H24) from CO2 and H2. In equation 14, CO2 is reduced to CO by the reverse water gas shift reaction. Then CO is converted to a theoretical minimum hydrocarbon chain length of eleven by the Fischer-Tropsch reaction shown in equation 15 [13]. The sum of equations 15 and 16 result in equation 17. Equation 17 shows the mole ratio of H2 to CO2 is 3.1 to 1, and laboratory results indicate that this ratio is necessary for efficient hydrocarbon production. 11CO2 + 11H2 11CO + 11H2O 11CO + 23H2 C11H24 + 11H2O 11CO2 + 34H2 C11H24 + 22H2O (15) Reverse water gas shift (16) Fischer Tropsch (17) Sum of equations 15 and 16 To produce feedstock ratios of 3:1 for future hydrocarbon production the current to the cell has to be increased over 4 times to 30 amps. At this current the hydrogen concentration will increase to 0.01 moles/min (equation 13), and the current to flow rate ratio will be decreased from 270 mL/amp to 63 mL/amp. From equations 14 through 16 and the calculated moles/min of CO2 and H2 given in Table 2 when the cell is operating at 30 amps, the maximum amount of synthetic 10PDF Image | Extraction CO2 H2 in Seawater Electrolytic Cation Exchange
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