Techno-Economic Assessment for CO2Capture From Air Using a Conventional Liquid-Based Absorption Process

In this study, the process of carbon dioxide (CO2) capture directly from ambient air in a conventional monoethanolamine (MEA) absorption process was simulated and optimized using a rate-based model in Aspen Plus. The process aimed to capture a specific amount (148.25 Nm(3)/h) of CO(2)from the air, which was determined by a potential application aiming to produce synthetic methane from the output of a 2.7 MW electrolyser (593 Nm(3)/h H-2). We investigated the technical performance of the process by conducting a sensitivity analysis around different parameters such as air humidity, capture rate defined as a ratio of moles of CO(2)captured during the process to the total mole of CO(2)in the feed stream, CO(2)loading of lean and rich absorption liquids and reboiler temperature, and evaluated the energy consumption and overall cost in this system. In order to meet the design requirement for standard packed columns, the rich absorption liquid was circulated to the top of the absorber. A capture rate of 50% was selected in this process as a baseline. At higher capture rates, the required energy per ton of captured CO(2)increases due to a higher steam stripping rate, required in the desorber, and at lower capture rates, the size of equipment, in particular, absorber and blowers increases due to the need for processing a significantly larger volume of air at the given CO(2)production volume. At the base case scenario, a reboiler duty of 10.7 GJ/tCO(2)and an electrical energy requirement of 1.4 MWh/tCO(2)were obtained. The absorber diameter and height obtained were 10.4 and 4.4 m, respectively. The desorber is found to be relatively small at 0.54 m in diameter and 3.0 m in height. A wash water section installed at top of the absorber decreased the MEA loss to 0.28 kg/ton CO2. However, this increased capital cost by around 60% resulting in CO(2)capture costs of $1,691 per ton CO(2)for the MEA base scenario. Based on the techno-economic analysis, assuming a non-volatile absorbent rather than MEA thereby avoiding a wash water section, and using an absorption column built from cheaper materials, the estimated cost per ton of CO(2)produced was reduced to $676/tCO(2). The overall cost range was between $273 and $1,227 per ton of CO(2)depending on different economic parameters such as electricity ($20-$200/MWh) and heat price ($2-$20/GJ), plant life (15-25 years) and capital expenditure (+/- 30%). In order to reduce the cost further, the use of innovative cheap gas-liquid contactors that operate at lower liquid to gas ratios is crucial.