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Simulated RTD curves

Figure 8 Simulated RTD curves using experimental density profile... Figure 8 Simulated RTD curves using experimental density profile...
Even though the model is in an development stage, it appears to be very attractive RTD curves can be computed along with the axial variations of the solid recirculation rate and of the average downward velocity of the solid in the annulus. Various parameters have been defined in the model, but no sensitive study has been performed extensively at this time. Only qualitative comparisons have been made between experimental and simulated RTD curves. [Pg.544]

It should be noted that a simulation results of the proposed solids transport model was used as a guide to determine when the dryer outlet stream should be sampled, in order to catch the peak of the residence time distribution (RTD) curve. In this way an information-rich signal was gained, which was invaluable for model validation and parameter estimation purposes, while at the same time reducing experimentation costs. [Pg.914]

It is important to mention that the present model is in a development stage. Only qualitative comparisons have been made between experimental RTD curves, expressed in term of the detector response, and the simulated responses expressed in term of the ratio L/Lq. Further investigations are required in order to perform a quantitative comparison between the detector response and L/Lq. [Pg.544]

The last elemenl of E , which is the collecting cell or outlet of the network, represents therefore the dynamic response of the system to a perturbation that may be a tracer impulse Eo=[l 0. .. 0]. Simulation of the RTD curve of the model is further performed by letting At become smaller and smaller until the stability of the solution is ensured. [Pg.687]

An Excel spreadsheet (Example8-7.xls) was used to determine the various RTD functions and the computer program PROGS 1 was used to simulate the model response curve with the experimental data. The results show the equivalent number of ideally mixed stages (nCSTRs) for the RTD is 13.2. The Gamma distribution function from Equation 8-143 is ... [Pg.755]

To establish the validity of the numerical scalar technique for RTD analysis, the normalized exit age distribution curve of both counter-current (Figure 1 (a-b)) and cocurrent (Figure 1 (c-d)) flow modes were compared. Table 1 shows that a good agreement was obtained between CFD simulation and experimental data. [Pg.670]

Computer program PROG81 determines the number of tanks, the variance, dispersion number, and the Peclet number from Hull and von Rosenberg data. The results of the simulation suggest that about three stirred tanks in series are equivalent to the RTD response curve. Figure 8-44 shows the shows E(0), FExp(0), and FModel(0) versus 0. [Pg.753]

The series-of-stirred-tanks model could not represent the RTD for the laminar-flow reactor shown in Fig. 6-7. However, the RTD data given in Example 6-2 can be simulated approximately. The dashed curve in Fig. 6-1 Oh is a plot of this RTD. While no integer value of n coincides with this curve for all 6/6, the curve for = 5 gives approximately the correct shape. Comparison of the fit in Figs. 6-9 and 6-lOh indicates that about the same... [Pg.259]

Fig. 6-11 Recording to the above equation for x, the area under the curve, from J 6) = 0 to J 6) = 1, is the conversion. Evaluation of this area gives x = 0.61. This is much closer to the plug-flow result of 0.63 than to the stirred-tank result of 0.50. The RTD for this case is shown in Fig. 6-1 Oh. This figure shows that not one, but five stirred tanks in series would best fit the RTD data. Thus the RTD comparison confirms that the single stirred tank would not provide a close simulation of the actual reactor. From this and the preceding example we have a good idea of how the RTD effects the conversion for first-order kinetics. The results are summarized in Table 6-1... Fig. 6-11 Recording to the above equation for x, the area under the curve, from J 6) = 0 to J 6) = 1, is the conversion. Evaluation of this area gives x = 0.61. This is much closer to the plug-flow result of 0.63 than to the stirred-tank result of 0.50. The RTD for this case is shown in Fig. 6-1 Oh. This figure shows that not one, but five stirred tanks in series would best fit the RTD data. Thus the RTD comparison confirms that the single stirred tank would not provide a close simulation of the actual reactor. From this and the preceding example we have a good idea of how the RTD effects the conversion for first-order kinetics. The results are summarized in Table 6-1...

See other pages where Simulated RTD curves is mentioned: [Pg.547]    [Pg.542]    [Pg.542]    [Pg.543]    [Pg.547]    [Pg.542]    [Pg.542]    [Pg.543]    [Pg.353]    [Pg.915]    [Pg.540]   
See also in sourсe #XX -- [ Pg.543 ]




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