Hydrogen production, Chapter costs

The (additional) costs of C02 capture in connection with hydrogen production from natural gas or coal are mainly the costs for C02 drying and compression, as the hydrogen production process necessitates a separation of C02 and hydrogen anyway (even if the C02 is not captured). Total investments increase by about 5%-10% for coal gasification plants and 20%-35% for large steam-methane reformers (see also Chapter 10). 

For the limitations of this publication, it is not possible to present a comprehensive set of the data used as input to the model. In principle, the model is based on the technoeconomic characteristics of hydrogen production and distribution technologies, as presented in Chapters 10 and 12, respectively, such as specific investments for certain plant sizes, full load hours, process efficiencies, maintenance and labour costs, etc. 

FIGURE 6-22 Estimated total annual fuel costs for light-duty vehicles possible future hydrogen production technologies (fossil fuels and nuclear energy), 2000-2050. See Table 5-2 in Chapter 5 and discussion in text. NOTE The cost curve for nuclear thermal energy (CS Nu-F) is obscured by the cost curve for distributed generation from natural gas (Dist NG-F), since these two cost estimates are virtually identical. 

FIGURE 6-23 Estimated total annual fuel costs for light-duty vehicles possible future hydrogen production technologies (electrolysis and renewables), 2000-2050. See Table 5-2 in Chapter 5 and discussion in text. 

If hydrogen production is based on surplus renewable energy such as wind power (as in the scenario in Chapter 5, section 5.5), the impacts are dramatically reduced. Only the occupational impacts are larger, at least at present, due to their roughly scaling with the cost of the conversion equipment, whether conventional electrolysers or reversely operated fuel cells. 

Look at the production of hydrogen by fermentation and on the basis of biomass from waste or from dedicated crops. Estimate current and possibly reduced future costs of such a hydrogen production system, taking into account the cost of bio-feedstock, its transportation as well as the hydrogen-producing conversion equipment (cf. Chapter 2, section 2.1.5). 

H2Sim compares the end-use cost of using hydrogen in either FCV or hybridized, direct hydrogen combustion vehicles in 2020 with today s internal combustion engine vehicles, hybrid, and electric vehicles. It also considers a 2020 FCV with onboard production of hydrogen. The default costs associated with each of the vehicles included in H2Sim were summarized in Table 8.1. This chapter focuses on the fuel and the total end-use costs associated with each vehicle based on fuel and vehicle cost sensitivity analysis. 

Rhodium catalyzed carbonylations of olefins and methanol can be operated in the absence of an alkyl iodide or hydrogen iodide if the carbonylation is operated in the presence of iodide-based ionic liquids. In this chapter, we will describe the historical development of these non-alkyl halide containing processes beginning with the carbonylation of ethylene to propionic acid in which the omission of alkyl hahde led to an improvement in the selectivity. We will further describe extension of the nonalkyl halide based carbonylation to the carbonylation of MeOH (producing acetic acid) in both a batch and continuous mode of operation. In the continuous mode, the best ionic liquids for carbonylation of MeOH were based on pyridinium and polyalkylated pyridinium iodide derivatives. Removing the highly toxic alkyl halide represents safer, potentially lower cost, process with less complex product purification. 

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