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720 kg/h of oxygen as by-product. It is assumed that the oxygen is made available to the market, without any further stream conditioning. Figure 13: Process flow diagram of FA synthesis from CO2 and H2 from electrolysis. 5.3.2 Reaction stage (Units 14-16) The reactor size has been assumed proportional to the batch reactor considered in the reported laboratory tests, scaled-up based on the inlet CO2 flowrate; the resulting size is about 18.5 m3. In the reactor vessel (unit 14), the liquid reaction of CO2 and H2 with the amine to form the FA-amine adduct, takes place under the presence of a ruthenium- and phosphino- based catalyst. The simplified reaction is expressed as: CO2 H2 C18H39NC18H39NHCOOH Eq. (13) The reactor is designed to reach a conversion of 19 % of the incoming H2. The unconverted H2 leaves the reactor in the gas phase, together with some unsolved CO2. The temperature of the reactor is fixed at 93 °C. Even though the reaction is exothermal, a small amount of steam is required to maintain the temperature at 93 °C (around 300 kW at 110 °C). The gas leaving the reactor is recycled back (stream 18) to the inlet with a compressor (unit 16), while a small gas percentage is purged to avoid the accumulation of unreacted (reactive and inert) components (stream 19; splitting fraction 1 % in mass basis). The recycle rate is highly dependent on the reactor temperature and the amount of CO2 solved in the liquid phase. This liquid phase (stream 20) has two well differentiated parts: a heavy phase, enriched with the adduct and the polar solvent, and a light phase, enriched with the tertiary amine (that is not combined to form the adduct) and the homogeneous catalysts. Free amine is present in both phases. See a diagram of this two phase liquid in Appendix 2, Figure 24. The partition coefficients have been estimated based on data from the patent [130], example A-12. 48PDF Image | evaluation of CO2 utilisation for fuel production
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