With a fixed value of 3 g of total catalyst loaded at the bottom of the reactor, in the first group, denoted as Group I, the Catalyst I was put in the upper of the catalyst bed with a loading amount of 0.5, 1.0, 1.5, 2.0, and 2.5 g, respectively.
For large saccharification reactors in the second step, the scale-up was easy because of no mixing mechanism was involved.
In both of the optimization states, to ensure the optimality and safety of the proposed arrangements during the cycle, the behavior of thermo-neutronic parameters of the reactor core in the second cycle was studied through time-dependent calculations.
The chemically treated effluent was then subjected to a biological oxidation reaction in the second reactor for further treatment with a residence time of 5 days.
In consequence, the conditional probability that an infected group was released to the destination farm was the probability of the group to have at least one infected animal given that all animals were negative reactors, also in the second serological testing round.
The Finns approved construction of a reactor in 2002, the first in western Europe for over a decade.
At least one of those pools, which are highly radioactive, was exposed by hydrogen explosions that destroyed the reactor buildings in the first days of the accident.
This is so, because for any given ethanol yield between 0 and 0.35, a horizontal line l extended from the yield value in the ordinate intersects the by-pass reactor trajectory in the first place.
The composition of catalysts varies, considering two applications in a multi-reactor system: a CoMo catalyst for the first reactor, and a NiMo in the second reactor; the former is supported on γ-Al2O3 and the latter on TiO2/Al2O3.
