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Environmental metrics (see Table 8 for conventional plant values) CO2not-emitted (tCO2/tFA) 2 CO2change (%) 92 From the mass balance in Table 6, feed streams are H2O to the electrolyser and CO2. There is an amount of O2 produced from the electrolysis process, sold as a by-product, a certain amount of unreacted water which is considered a by-product for disposal, and off-gases or purge gases resulting from the FA separation processes. The energy needs outlined in Table 6 indicate that the FA CDU plant requires electricity, cooling water and steam. The total electricity consumption for compression (CO2, H2 and recycled gas streams) and pumping, and the requirement of the electrolysis process is about 4 MWh/tFA. The cooling water needed is 252 t/tFA, while steam needs are 3.7 t/tFA for HP steam, and 2 t/tFA for MP steam. The reactor conversion is 19 % for H2 and 81 % for CO2; while the whole process converts 98 % of inlet CO2 and 63 % of inlet H2. From this is derived an amount of CO2 used of 0.668 t/tFA, only if renewable steam and electrolysis are considered (as described in the methodology, the metric CO2 used, as a design condition, has to be positive). Table 7 summarises the value of the net CO2 used if steam and/or electricity do not come from renewable sources. Note that "zero" CO2 emissions sources are crucial to achieve an FA CDU process with net CO2 emissions reduction. Otherwise, the process generates more CO2 emissions than the ones utilised as raw material. From now on, the emissions related to the FA CDU process will consider zero CO2 emissions sources for the electricity needed for electrolysis and for the generation of steam. Table 7: Variation of CO2 used, combining zero CO2 emissions allocated to electricity and/or steam, and emissions derived from 0.508 tCO2/MWh electricity [113], and 0.072 tCO2/GJ steam [43] . Indirect CO2 emissions are allocated to steam and electricity needs of the electrolyser Indirect CO2 emissions are only allocated to electricity needs of the electrolyser Indirect CO2 emissions are only allocated to steam needs Indirect CO2 emissions are zero tCO2/tFA -1.970 -1.249 -0.054 0.668 Figure 15 and Figure 16 depict the breakdown of costs. Among the investment needed (Figure 15), the electrolyser represents 43 % of the total ISBL. It is followed by the contributions from the compression system and the separation processes. If compared with the MeOH plant results, it is noticed that the cost of electrolysis has a relatively lower contribution in the overall share of investment costs. This is due to stoichiometry of the system formed by Eq. (13) and Eq. (14): the reaction to synthesise one mole of FA needs one mole of H2, while MeOH needed three moles of H2 per mole of product. The second larger contributor to the investment in the FA plant is compression, as feed streams to the reactor need to be compressed up to 105 bar. In this case, the importance of the HEX is lower than in the MeOH plant since as demonstrated by the pinch point analysis, no significant heat integration was possible. In the FA synthesis process the separation processes are important to recover catalysts and solvents, resulting in more separation steps than for MeOH purification. Figure 16 points out that consumables and utilities (electricity and steam) are the main contributors to the production costs. As shown in Table 6, the calculated BCR calculated at 0.43, underlines the need to compensate the high variable costs (production costs are more than twice the benefits obtained). The GM is EUR 7.7 million/yr, which means that revenues and by-product benefits are larger than raw materials cost. 54PDF Image | evaluation of CO2 utilisation for fuel production
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