• Energy Research

Abstract Application of process intensification (PI) technologies such as rotating packed beds (RPBs) to replace packed beds (PBs) in solvent-based CO 2 capture could reduce plant footprint. Concentrated monoethanolamine (MEA) solvents are generally expected to be used in RPBs. Under this circumstance, expected temperature rise during CO2 absorption should be estimated to determine whether or not intercooling is necessary for RPBs. In this study, we demonstrated that intercooling is inevitable with RPBs using 40-70 wt% monoethanolamine (MEA) solvent through liquid phase energy balance for a hypothetical scenario. Our analysis showed that liquid phase temperature rise could be as high as 80°C in some cases and this will significantly reduce absorption rate without intercooling.

Abstract Application of process intensification (PI) technologies such as rotating packed beds (RPBs) to replace packed beds (PBs) in solvent-based CO 2 capture could reduce plant footprint. Concentrated monoethanolamine (MEA) solvents are generally expected to be used in RPBs. Under this circumstance, expected temperature rise during CO2 absorption should be estimated to determine whether or not intercooling is necessary for RPBs. In this study, we demonstrated that intercooling is inevitable with RPBs using 40-70 wt% monoethanolamine (MEA) solvent through liquid phase energy balance for a hypothetical scenario. Our analysis showed that liquid phase temperature rise could be as high as 80°C in some cases and this will significantly reduce absorption rate without intercooling.

This paper promotes awareness of the circular economy as a superior waste disposal system alternative. The novelty of this study is to model cleaner energy generation from the gasification of polyethene terephthalate (PET) waste accompanied by a detailed analysis on the economic feasibility. In the approximate analysis of PET, the percentage values for Ash and hydrogen were low (0 and 4.21, respectively). This parameter significantly impacted the Ash and hydrogen contents of the output gas, as it directly influenced the PET feedstock to a more excellent heating value (23.34 MJ/kg) and lower heating value (10.63 MJ/kg). Temperature and pressure are treated as free variables throughout each block during the gasification procedures. A sensitivity study revealed that the PET moisture content has no significant effect on the product composition. The economic analysis indicated that the gasification process could be economically viable. The economic analysis of the process considered the comprehensive evaluation of the plant’s financial aspects. The economic evaluation indicated that the facility would reach the break-even point by the end of its third year of operation, demonstrating its economic viability, with an NPV of £77,574,506.37 and an ROI of 40.1% for the suggested 25-year operational period of the facility.

This paper promotes awareness of the circular economy as a superior waste disposal system alternative. The novelty of this study is to model cleaner energy generation from the gasification of polyethene terephthalate (PET) waste accompanied by a detailed analysis on the economic feasibility. In the approximate analysis of PET, the percentage values for Ash and hydrogen were low (0 and 4.21, respectively). This parameter significantly impacted the Ash and hydrogen contents of the output gas, as it directly influenced the PET feedstock to a more excellent heating value (23.34 MJ/kg) and lower heating value (10.63 MJ/kg). Temperature and pressure are treated as free variables throughout each block during the gasification procedures. A sensitivity study revealed that the PET moisture content has no significant effect on the product composition. The economic analysis indicated that the gasification process could be economically viable. The economic analysis of the process considered the comprehensive evaluation of the plant’s financial aspects. The economic evaluation indicated that the facility would reach the break-even point by the end of its third year of operation, demonstrating its economic viability, with an NPV of £77,574,506.37 and an ROI of 40.1% for the suggested 25-year operational period of the facility.

Abstract For large volumes of carbon dioxide (CO 2 ) onshore and offshore transportation, pipeline is considered the preferred method. This paper presents a study of the pipeline network planned in the Humber region of the UK. Steady state process simulation models of the CO 2 transport pipeline network were developed using Aspen HYSYS®. The simulation models were integrated with Aspen Process Economic Analyser® (APEA). In this study, techno-economic evaluations for different options were conducted for the CO 2 compression train and the trunk pipelines respectively. The evaluation results were compared with other published cost models. Optimal options of compression train and trunk pipelines were applied to form an optimal case. The overall cost of CO 2 transport pipeline network was analyzed and compared between the base case and the optimal case. The results show the optimal case has an annual saving of 22.7 M€. For the optimal case, levelized energy and utilities cost is 7.62 €/t-CO 2 , levelized capital cost of trunk pipeline is about 8.11 €/t-CO 2 and levelized capital cost of collecting system is 2.62 €/t- CO 2 . The overall levelized cost of the optimal case was also compared to the result of another project to gain more insights for CO 2 pipeline network design.

Abstract For large volumes of carbon dioxide (CO 2 ) onshore and offshore transportation, pipeline is considered the preferred method. This paper presents a study of the pipeline network planned in the Humber region of the UK. Steady state process simulation models of the CO 2 transport pipeline network were developed using Aspen HYSYS®. The simulation models were integrated with Aspen Process Economic Analyser® (APEA). In this study, techno-economic evaluations for different options were conducted for the CO 2 compression train and the trunk pipelines respectively. The evaluation results were compared with other published cost models. Optimal options of compression train and trunk pipelines were applied to form an optimal case. The overall cost of CO 2 transport pipeline network was analyzed and compared between the base case and the optimal case. The results show the optimal case has an annual saving of 22.7 M€. For the optimal case, levelized energy and utilities cost is 7.62 €/t-CO 2 , levelized capital cost of trunk pipeline is about 8.11 €/t-CO 2 and levelized capital cost of collecting system is 2.62 €/t- CO 2 . The overall levelized cost of the optimal case was also compared to the result of another project to gain more insights for CO 2 pipeline network design.