Optimum operation line

Optimum Operating Line. The relationships between the conversion and the average molecular weight can be plotted as a function of initiator concentration while varying the jacket temperature to optimize the conversion. The relationships are shown in... 

Figure 5. Molecular weight-conversion contour map for various concentrations of a free-radical initiator operating in a tubular-addition polymerization reactor of fixed size. Curves were constructed using varying jacket temperatures (kinetic parameters for the initiator Ea = 32.921 Kcal/mol In k/ = 26.494 In sec f = 0.5 (------------------------) optimum operating line)...

Optimum Operating Lines of Continuous Ideal Non-isothermal Reactors... 

The situation is different for exothermic reversible reactions (Figure 4.10.34c), as now two opposing factors are at work. The rate of the forward reaction speeds up with temperature but the maximum attainable conversion decreases. Consequently, we start at a high temperature and then reduce the temperature as conversion rises. The optimum operation line is found by connecting the maxima of the rate curves (Example 4.10.2). 

Optimum Operation Line for Adiabatic Operation The relations between conversion, temperature, and rate of reversible reactions in an adiabatic PFR and a CSTR are given schematically in Figure 4.10.36. For a constant value of Cp, we obtain ... 

Optimum Operation Line for Non-adiabatic Operation of a PFR For a reversible exothermic reaction in a PFR, the optimum operating line (Figure 4.10.34c) can only be reached if we remove heat along the tube, as examined in Example 4.10.4. 

Fig. 8.6 Optimum operating line of temperature at the continuous heat-exchange...

Fig. 8.7 Optimum operating line of temperature of the adiabatic fixed-bed reactor...

Fig. 6A, B and C show operating lines for the three types of reactors in methanol synthesis (confer Table 4, case 2). The situation is the same here. The internally cooled reactor gives the best approach to the optimum operating line and may as a consequence be designed for the smallest catalyst volume, whereas the quench cooled reactor requires the largest volume. It is not, however, possible to base a choice between the reactor types solely on the required catalyst volume. As indicated in Table 1, a number of other considerations must be taken into account.

Operating line, humidifying towers 778 Optimum pipe diameter, example 371 — water velocity, heat exchanger 505 Orifice meter 244,246, 248... 

Real-time synthesis of operating procedures. Most of the ideas and methodologies, presented in this chapter, are applicable to the a priori, off-line, synthesis of operating procedures. There is a need though to address similar problems during the operation of a chemical plant. Typical examples are the synthesis of operational response (i.e., operating procedure) to process upsets, real-time recovery from a fallback position, and supervisory control for constrained optimum operation. 

The atomic absorption characteristics of technetium have been investigated with a technetium hollow-cathode lamp as a spectral line source. The sensitivity for technetium in aqueous solution is 3.0 /ig/ml in a fuel-rich acetylene-air flame for the unresolved 2614.23-2615.87 A doublet under the optimum operating conditions. Only calcium, strontium, and barium cause severe technetium absorption suppression. Cationic interferences are eliminated by adding aluminum to the test solutions. The atomic absorption spectroscopy can be applied to the determination of technetium in uranium and its alloys and also successfully to the analysis of multicomponent samples. 

Using this modified operating line, the procedure for finding the reactor size and optimum operations follows directly from the discussion on adiabatic operations. 

For operating line CD of Example 9.6 we find an optimum recycle area, shown in Fig. E9.7 as rectangle EFGH. 

Thus, the main function of the DOC is to oxidize CO and unburned HCs. The secondary function, utilized in combined exhaust aftertreatment systems, is the oxidation of NO to N02, which then enables optimum operation of the NOx aftertreatment catalysts placed down the exhaust line (NSRC and/or SCR, cf. Sections VI, VII and VIII, and also DPF). 

For the optimum operation and control, reliable on-line sensing devices need to be developed. On-line optimization algorithms need to be developed and used to enhance the operability of bioprocess and to ensure that these processes are operated at the most economical points. 

To determine the optimum feed plate location, draw a line from the feed composition on the y = x line, through the intersection of the top/bottom operating lines, to the equilibrium curve. The step straddling the feed line is the correct feed-plate location. 

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