Reactor process, graph

Comparing the lower graphs in Figures 16.7 and 16.8 shows that the break-even point between the reactive distillation and column/side reactor process moves from an of about 1.5 down to about 1.4. 

Sci Finder scholar search, keyword microwave not spectroscopy ). The black graphs represent the number of publications (2001—2004) reporting MAOS experiments in dedicated reactors with adequate process control (ca. 50 journals, full text search microwave). 

Hint It may help to first draw a qualitative graph which shows the different processes as a function of the concentration in the reactor, C. 

To do this we will load a helpful package called Miscellaneous Units from Mathematica. We also want graphs of the predicted catalyst mass as function of time, the theoretical level of catalytst in the reactor as a function of time, and the actual level that has been measured in the reactor at a few times during the loading process. Finally, we can compute the catalyst cost in flowing into the reactor volume per unit time. Here we calculate the mass flow in per unit time in metric units as well as the volume and cross-sectional area of the reactor. 

Figure 6.32. Plot of the reciprocal of the reaction rate, l/rj, as a function of the concentration, Cj, as a measure of conversion. The processes shown in graphs a-c correspond to Fig. 6.31 a-c, which may be used in evaluating the mean residence time for a continuous stirred vessel CSTR or a tubular reactor CPFR with Equs. 6.77 and 6.78. A combination of a CSTR with a CPFR is shown to be optimal in case c (stage I is a CSTR and stage II is a CPFR). (Figures 6.32a and 6.32b adapted from Levenspiel, 1972 Figure 6.32c adapted from Topiwala, 1974).

Graphs of Eq. (8.35) shown in Fignre 8.7 demonstrate that this scheme could work for Co because precipitating 20% of the Ca wonld remove nearly 50% of the Co. Using a series of mixed flow reactors would further improve the process because removal of 50% of the remaining Co in a second reactor would leave 25% and a third reactor would further reduce the Co to 12.5%. On the other hand, this process would be inefficient for Sr because precipitating 80% of the Ca would only remove about 10% of the Sr. Hence, co-precipitation in a mixed flow reactor is only effective for trapping trace elements if A > 1. 

The following graph in Figure 6.10 details the particle size distribution of titanium dioxide particles that results from a reactor with the following process parameter fixed at Tpr=40 °C and Tfnm = 900 °C. By varying the Qp the particle size distribution and the number concentration can be controlled. 

Assume that the feed to the reactor is 108 kmol/h propylene, 8 kmol/h propane, and 203 kmol/h benzene. The pressure is kept constant at 3000 kPa. Prepare performance curves on the same graph for temperatures from 350°C to 400°C in 10°C intervals. Superinpose on this graph the maximum allowable conditions, which correspond to a steam-side pressure of 4800 kPa. A process simulator should be used to generate points on the performance curves. Other data reactor volume = 7.89 m, heat transfer area A = 436 m, overall heat transfer coefficient = 65 W/m °C. 

The graph zone represented in Fig. 2.12 shows that the kinetic curve of the source reactant has a characteristic feature in the course of time the concentration becomes time-constant. We met the similar curve behaviour when analyzing reversible reactions however, in this case, stabilization of the concentration with time is not related to establishing the chemical equilibrium state. In the case under consideration, we have a steady-state regime of the process, a state when a reactant loss because of proceeding a reaction is precisely compensated by its gain at the expense of feed of new reactant portions to a reactor. The expression for the steady-state concentration of substance A is easily reduced by equating the derivative in (2.7) to zero... 

It will be clear from the graph V ==/i(Fi) of the recycling process and the graph Vi- -Vz— /s(Fi) of the two-stage system, that if the degree of conversion in one cycle equals 0-7 or less, the volume of the reactor of the recycling system will be far lower than the minimum volume of the two-stage system. 

The computer system of JRR-3M consists of a management computer system and a process computer system The management computer system works mainly for reactor-operation-data logger and plays some roles to print out the operation data, display a trend graph of process variables and store the data The process computer system works to support start-up and shut-down procedures of the reactor and manage data from process instrumentation... 

---