## 1 Introduction  
Hydrogen can be produced on a large scale from conventional hydrocarbon sources through steam reforming, partial oxidation, gasification, and from renewable energy (including solar, wind, and hydro power) through electrolysis [1]. Owing to the massive expansion and the intermittent nature of renewable power, the production, storage, and transportation technologies related to green hydrogen with improved economic returns need to be developed. Potential improvements and the physical limitations of various hydrogen storage methods have been reviewed [2, 3]. Among the various hydrogen storage technologies, liquid organic hydrogen carrier (LOHC) systems are considered a feasible option due to their reasonable hydrogen storage capacity and ability to be transported under ambient conditions [4]. Moreover, because the carrier compounds do not release unwanted hydrogen without suitable catalysts, the existing storage and transport infrastructure for the oil industry can be employed [5, 6]. Although detailed descriptions of LOHC technologies can be found in the existing literature [7, 8], information required to understand the discussions in the present investigation is provided in the following sections. Transport over long distances and storage during extended periods are realized based on a two-step cycle of LOHC technology. The first step is catalytic hydrogenation, which involves loading hydrogen into carrier molecules to produce LOHC+. The second is catalytic dehydrogenation, which involves releasing hydrogen from the LOHC+ to recover the hydrogen depleted carrier (LOHC\(-\)), which is then recycled back to the hydrogenation site to repeat the cycle [4]. The hydrogenation of the carrier is an exothermic reaction, while dehydrogenation is an endothermic reaction. The heat released by the exothermic reaction and the heat demand of the endothermic reaction are identical and are dependent on the carrier compound. The enthalpy varies between 50.6 and 72.0 kJ/mol H\({}_{2}\) for the most common carriers. The reaction conditions also vary for different compounds, although dehydrogenation of the carrier is generally performed at relatively lower pressures (approx. 1 atm) and relatively higher temperatures (270-350 \({}^{\circ}\)C). In contrast, hydrogenation is conducted at higher pressures of 50-70 bar and lower temperatures of 100-250 \({}^{\circ}\)C. The reactions also require supported noble metal catalysts. For example, Ru and Pt on an Al\({}_{2}\)O\({}_{3}\) support can be used for the hydrogenation and dehydrogenation of the LOHC. The primary barriers before LOHC technology can be commercialized are the supply of huge reaction enthalpy at increased temperatures and the slow reaction rate during dehydrogenation. Accordingly, the feasibility of coupling high-temperature waste heat from a solid oxide fuel cell or a methanation process to supply LOHC dehydrogenation energy has been investigated [9]. The existing plug flow reactor (PFR) and packed bed reactor (PBR) for LOHC technology suffer from prolonged dehydrogenation [7; 10]. This is probably caused by either delayed heat and mass transfer [11] or complex reaction mechanisms [12]. LOHC degradation at elevated temperatures is an additional serious obstacle [13; 14]. The present study focused on boosting the speed of dehydrogenation using a developed triple-loop dehydrogenation system, which is composed of a \"reaction loop\", a \"heating loop\", and a \"chilling loop\". Preliminary gas infiltration, flow visualization, and reactor pumping experiments were conducted to determine the core parameters of the reaction loop, which were based on a rotating packed bed-type reactor. The concepts, construction, and experimental results are described in the following subsections. The suggested design of the heating loop provides diagnostics for the LOHC degradation problem by minimizing the temperature difference between the heating surface and adjacent LOHC liquid.