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2 METHODOLOGY This section summarises the systematic methodology used to evaluate the potential impact of the CDU options addressed in this report. This work utilises process flow modelling to obtain the energy and mass balances, the total purchase cost of the equipment of both CDU plants and all the derived parameters for the technological, economic and environmental evaluation of each plant. From the modelling task, the NPV and the tonnes of CO2 consumed per tonne of product are the main input to financial and market analyses. Overall, this report combines modelling; technological, economic and environmental metrics evaluation; comparison with the equivalent conventional process to produce each fuel; study of the profitability through sensitivity analyses of the most important variables; and an estimation of market prospects. Assumptions made in this report (and described in the following sections): Gate-to-gate analysis: CO2 emissions upstream or downstream the CDU process are not considered. Zero CO2 emissions sources (renewables, in general, in this report) have no emissions allocated to them. This is a simplification, since only direct emissions are zero. There are however indirect emissions over the life cycle. "Expensive" CDU plants are of concern: this includes CO2 conditioning (pressurisation and purification) and H2 synthesis. Consideration of the worst case scenario for benchmark plants: electricity and steam are assumed to be provided by the European energy mix. 2.1 Process modelling, total purchase cost and variable cost of production A conceptual design of each selected process is implemented in the software modeller CHEMCAD, according to an average commercial plant size. Every carbon dioxide utilisation technology is at different TRL (see Table 1), that is translated into more or less uncertainty in the modelling and scaling-up process. The boundaries of the CDU plant and thus of the model, are set on the utilisation plant itself; CO2 capture and transport are outside these boundaries. The CDU plant is compared with the benchmark process of synthesis, which uses a fossil fuel instead of CO2 as its raw material. Figure 1 represents the boundaries and the main inlet and outlet streams of both, CDU and conventional plants. The analysis is performed gate-to-gate. The carbon utilisation plant includes inside its boundaries (see Box 3) the electrolysis process to obtain H2, since H2 is a reactant in the MeOH and FA plants; the CO2 purification process, to avoid catalyst poisoning, and CO2 compression previous to the synthesis process. It is assumed that the captured CO2 is available at ambient conditions and needing further purification, as a worst case scenario (i.e. the CDU plant takes care of all the CO2 conditioning). As for the H2 production, water electrolysis is a synthesis alternative to keep CO2 emissions as low as possible [51]; moreover, systems of hydrogen supply are not yet fully implemented [52]. Electrolysis and CO2 purification units are modelled as black box units and their investment costs are estimated using available figures in literature: Bolat and Thiel [52] for the electrolyser, and Heyne and Harvey [53] for the purification unit. As two catalytic processes are considered in this report, we assume that feedstock CO2 has to be 99.99 % pure. The total purchase cost of the equipment is estimated with CHEMCAD and also using the design criteria of Towler and Sinnott for heat exchangers cost estimation [54]. It is assumed that the 23PDF Image | evaluation of CO2 utilisation for fuel production
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