Modeling and optimization of an industrial hydrogen unit in a crude oil refinery |
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| Affiliation: | 1. Clean Energy Research Lab (CERL), Department of Physics, COMSATS University Islamabad, Lahore Campus, Lahore 54000, Pakistan;2. University of Education, Township, Lahore 54000, Pakistan;3. Sustainable Energy Technologies Center, King Saud University, Riyadh, Saudi Arabia;4. University of Okara, Okara, Pakistan;1. Institute for Advanced Materials, Hubei Key Laboratory of Pollutant Analysis &Reuse Technology, Hubei Normal University, Huangshi 435002, China;2. The State Key Laboratory of Refractories and Metallurgy, College of Materials and Metallurgy, Wuhan University of Science and Technology, Wuhan 430081, China;3. National Laboratory of Solid State Microstructures, Nanjing University, Nanjing 210093, China;1. Lehigh Carbon Community College. Schnecksville, PA, 18078, USA;2. Department of Chemistry and Biochemistry, Duquesne University, Pittsburgh, PA, 15282, USA;1. TÜBİTAK Marmara Research Centre Energy Institute, Kocaeli, Turkey;2. Istanbul Technical University, Mechanical Engineering Department, İstanbul, Turkey;1. Department of Chemical Engineering, Faculty of Engineering, Ferdowsi University of Mashhad, Mashhad, Iran;2. Department of Chemical Engineering, Laval University, Quebec, Canada;3. Department of Chemical Engineering, Shiraz University, Shiraz 71345, Iran |
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| Abstract: | The main goal of this research is the modeling and optimization of an industrial hydrogen unit in a domestic oil refinery at steady state condition. The considered process consists of steam methane reforming furnace, low and high temperature shift converters, CO2 absorption column and methanation reactor. In the first step, the reactors are heterogeneously modeled based on the mass and energy balance equations considering heat and mass transfer resistances in the gas and catalyst phases. The CO2 absorption column is simulated based on the equilibrium non-ideal approach. In the second step, a single objective optimization problem is formulated to maximize hydrogen production in the plant considering operating and economic constraints. The feed temperature, firebox temperature, and steam flow rate in the reformer, feed temperature in shift converters, lean amine flow rate in the absorption column, and feed temperature in the methanator are selected as decision variables. The calculated effectiveness factors and mass transfer coefficients prove that the methane reforming is inertia-particle mass transfer control, while shift and methanation reactions are surface reaction control. The simulation results show that applying the optimal condition on the system increases hydrogen production capacity from 85.93 to 105.5 mol s−1. |
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| Keywords: | Hydrogen production Steam methane reforming Shift converter Methanator Heterogeneous modeling Optimization |
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