Microchannel steam reforming reactors with insulating wall materials for hydrogen production Junjie Chen Department of Energy and Power Engineering, School of Mechanical and Power Engineering, Henan Polytechnic University, 2000 Century Avenue, Jiaozuo, Henan, 454000, P.R. China Contributor: Junjie Chen, ORCID: 0000-0001-5055-4309, E-mail address: komcjj@gmail.com In one form, the design includes a monolithic catalytic reactor with a primary flow path comprising a number of tubes which are lined with a catalyst. As chemical reactants are fed into the primary flow path the chemicals react, with the aid of the catalyst, to produce an exothermic reaction. In the same catalytic reactor is a secondary flow path, also comprising a number of tubes and also lined with a catalyst. In this secondary flow path, a different collection of chemical reactants are fed and, through the aid of the catalyst, will produce an endothermic reaction. The tubes of the primary and secondary flow paths are interspersed with one another within the monolith such that the heat generated from the exothermic reaction may conduct through the tube walls and serve as a heat source for the endothermic reaction. Furthermore, the microchannel steam reforming reactor design includes a method for enhancing one or more catalytic chemical reactions in terms of rate, product yield, energy and other parameters. Here, the initiating an exothermic reaction within one flow path of the monolithic reactor serves the dual purpose of creating a product yield as a result of that exothermic reaction and as a heat source. With the aid of this heat source, a second and endothermic reaction may be initiated in a secondary flow path which may absorb the heat from the exothermic reaction thereby enhancing product yield and making efficient use of available energy. To optimize the use of this heat, the reactions are controlled through one of many factors such as feed rate of the reactants, catalyst quality, reactant concentration and others. The flow paths may be co-current, countercurrent or other such variation as necessary to maximize heat transfer between the two reactions. Streamwise distance (meter), Heterogeneous reaction rate along the length of the reactor (mole per square meter per second) 0 8.97706 0.00025 9.12983 0.0005 9.45292 0.00075 9.76459 0.001 10.009 0.00125 10.1761 0.0015 10.2678 0.00175 10.2901 0.002 10.2514 0.00225 10.1611 0.0025 10.0284 0.00275 9.86268 0.003 9.67153 0.00325 9.46156 0.0035 9.23929 0.00375 9.01005 0.004 8.77805 0.00425 8.54661 0.0045 8.31863 0.00475 8.09598 0.005 7.87987 0.00525 7.67157 0.0055 7.47194 0.00575 7.28144 0.006 7.10033 0.00625 6.92886 0.0065 6.76695 0.00675 6.61432 0.007 6.47076 0.00725 6.33601 0.0075 6.20963 0.00775 6.09103 0.008 5.98024 0.00825 5.87692 0.0085 5.78047 0.00875 5.6906 0.009 5.60703 0.00925 5.5293 0.0095 5.45708 0.00975 5.38993 0.01 5.3273 0.01025 5.26922 0.0105 5.2156 0.01075 5.1662 0.011 5.12058 0.01125 5.07842 0.0115 5.03943 0.01175 5.00345 0.012 4.9703 0.01225 4.93973 0.0125 4.91161 0.01275 4.88587 0.013 4.86227 0.01325 4.84055 0.0135 4.82058 0.01375 4.80242 0.014 4.78598 0.01425 4.77087 0.0145 4.75708 0.01475 4.74449 0.015 4.73297 0.01525 4.72248 0.0155 4.71307 0.01575 4.70472 0.016 4.69726 0.01625 4.69071 0.0165 4.68471 0.01675 4.67933 0.017 4.67489 0.01725 4.67115 0.0175 4.66781 0.01775 4.66491 0.018 4.6626 0.01825 4.66054 0.0185 4.65865 0.01875 4.65713 0.019 4.65599 0.01925 4.65505 0.0195 4.6543 0.01975 4.65386 0.02 4.65375 0.02025 4.65363 0.0205 4.6535 0.02075 4.6538 0.021 4.65451 0.02125 4.65516 0.0215 4.65575 0.02175 4.65657 0.022 &

Contributor: Junjie Chen, ORCID: 0000-0001-5055-4309, E-mail address: komcjj@gmail.com, Department of Energy and Power Engineering, School of Mechanical and Power Engineering, Henan Polytechnic University, 2000 Century Avenue, Jiaozuo, Henan, 454000, P.R. China