###### Abstract
The objective of this research is to find the feasible layout and storage pressure that minimize the capital and operation cost of H\({}_{2}\) and CO\({}_{2}\) gas compression and storage vessels. Regarding H\({}_{2}\) compression and storage, the main research has focused on the thermodynamic analysis of filling hydrogen storage tanks and the influence of temperature evolution. The effects of heat losses and filling rate optimization for a refuelling gaseous fuel tank was studied by [PERSON] et al. [11]. Their objective was to compare the temperature and pressure evolutions coming from different equations of state and from thermodynamic tables. They optimized the filling rate to minimize heat losses in a tank up to 270 bar. A similar analysis was developed elsewhere [12; 13]. In this work [12], a parametric study was performed to analyse the effect of the initial conditions on the exergy destruction and efficiency of the filling processes. The focus was on the transient filling process and determined temperature and pressure changes inside the storage tank during filling. The final pressure was 350 bar and the initial pressure varied between 5 and 20 bar. Similar objectives were showed by [PERSON] et al. [13]. [PERSON] et al. reviewed the research on the H\({}_{2}\) filling procedure [14], which is a hot topic for the H\({}_{2}\) and electrolyser industry. The compression work input for different compression processes were previously analysed by [PERSON] et al. [15]. The percentage of LHV for hydrogen compression varies between 5 and 20% for pressures up to 600 bar, depending on an ideal isothermal or adiabatic compression. This huge variation, 400% in energy requirement, emphasizes the necessity of a particular study for each H\({}_{2}\) application where the process compression configuration was also studied. CO\({}_{2}\) compression was mainly investigated in relation to Carbon Capture and Storage (CCS) applications. [PERSON] et al. [16] studied the power requirements for CO\({}_{2}\) compression and the minimization of energy requirements through intercooling compression. These power requirements could be as much as 100 kWe per tonne CO\({}_{2}\) and it is a key issue for the feasibility of this system. They proposed the integration of intercooling CO\({}_{2}\) compression into the low-pressure part of a steam cycle to take advantage of the intercooling heat and analysed the energetic and economical results, finding a reduction in the compression power requirement of around 40%. Several researches have also work on this topic for CCS. [PERSON] and [PERSON] [17] made a theoretical approach and analysed the heat and work integration and its application to CCS. [PERSON] et al. [18] developed an advanced exergy analysis of a CO\({}_{2}\) pressurization strategy. [PERSON] et al. [19] studied the utilization of compression heat with regenerative steam Rankine cycles and [PERSON] et al. [20] with Organic Rankine Cycle (ORC) to minimize the energy requirements. As in the case of H\({}_{2}\), the analysis of CO\({}_{2}\) compression depends strongly on the final application. For CCS applications, the objective is gas transportation from the source to the storage site. Generally, the gas is transported in supercritical conditions or condensed below its critical point. [PERSON] and [PERSON] [21] made a comparison of the energy consumption associated with compression process alternatives. The main finding was that the performance advantages claimed for improved CO\({}_{2}\) compression process schemes are often optimistic. It requires a detailed simulation of the process with performance data provided by a commercial CO\({}_{2}\) compressor manufacturer, analysis of transient performance [22], and include the limitations caused by composition, safety, and transportation options (pipelines and ships) [23].