Equations other equipment Table

Finally, some equipment is unaffected by pressure. Exaiiples are tower trays and packing. This equipment is not subjected to significant differential pressure because it is surrounded by process fluid. Therefore, in Equation A.3. use 0 = 2= C3 = 0. Some other equipment also has zero for these constants. For exarrple, conpressor drives are not exposed to the process fluid and so are not significantly affected by operating pressure. Other equipment, such as conpressors, do not have pressure corrections because such data were not available. Use of these cost correlations for equipment outside the pressure range shown in Table A.2 should be done with extreme caution. 

Equation A.4 and the data in Table A.4. For other equipment, the form of the equation is given in Table A.5. 

In addition to the requirements of processing so much feed and solvent with a required number of theoretical stages, there are the practical considerations concerning contamination, entrainment, emulsification, floor space, height requirements, cleanability, and versatility to handle other than design rates. The suitability of various type extractors with respect to each of these considerations is listed in Table 3. Not all of the features compared in the table can be equated. The tabulation is provided to show comparisons to aid in the selection of suitable equipment. 

The presumption in Equation 3.1 is that there is only one error structure to worry about. That is, it presumes that all experiments are run in such a way that they differ only with respect to changes associated with various levels of the factors. This would be likely with randomized runs occurring over a short span of time but unlikely if, for example, half the experiments were run in January and the other half in October. Unknown factor variations in feedstock, ambient conditions, differences in equipment used, and so on could all affect the results. If, however, we can presume that Equation 3.1 is an accurate model, then we can estimate the statistical significance of each coefficient. To do this, let us consider the example given in Table 3.2. 

Equipment design procedures for separation operations require phase enthalpies and densities in addition to phase equilibrium ratios. Classical thermodynamics provides a means for obtaining all these quantities in a consistent manner from P-v-T relationships, which are usually referred to as equations of state. Although a large number of P-v-T equations have been proposed, relatively few are suitable for practical design calculations. Table 4.2 lists some of these. All the equations in Table 4.2 involve the universal gas constant R and, in all cases except two, other constants that are unique to a particular species. All equations of state can be applied to mixtures by means of mixing rules for combining pure species constants. 

Table 16.32 Purchase Costs (f.o.b.) of Other Chemical Processing Equipment, CE Index = 394. Equations for pumps, compressors, motors, heat exchangers, and pressure vessels are in Section 16.5 ... 

Nevertheless, the method compares quite well with the other systems in several respects. The figmes in Table 8.18 below are calculated for a self-contained system capable of producing 1 kg of hydrogen, using the sodium hydride system. The equipment for containing the water and gas, and the cutting and control mechanism is assumed to weigh 5 kg. There is three times as much water as equation 8.14 would imply is needed. 

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