[...]... McGraw-Hill Companies All rights reserved Any use is subject to the Terms of Use as given at the website The Database 14 Chapter One Figure 1.4 RK.mak screen Industrial Chemical Process Design is indeed a toolkit offering the user practical process engineering Having covered the difficulties of deriving an accurate gas density in Eqs (1.15) and (1.16), it is important here to understand the practical... for figure curve reading with interpolation is again a reasonable check I submit therefore that MW or BP interpolation of Table 1.10 is sufficient You have now come to the finish of the Industrial Chemical Process Design database I resubmit that these 8 data properties (viscosity, ... decreases A conservative approach would be to use a larger Z than calculated or assume Z = 1.0 for a safe and conservative design In most cases no line size increase results, while in some cases only one line size increase is the outcome I suggest this is good practice I have designed many flare systems and performed numerous emergency relief valve sizing calculations applying this Z = 1.0 criterion... estimate can be made for most other components by relating them to the family types listed in Table 1.3 Also included here is an equation for calculating TC, °R, using SG 60/60 and the boiling point of the unknown HC The constants A, B, and C are given for paraffins and aromatic-type families For naphthene, olefin, and other family-type HCs A, B, and C constants, the process engineer is referred to the API... good for paraffins up to 21 carbon atoms molecularly, and up to 15 carbon atoms for all others Now for the best resource of all Table 1.3 has many applications In recent years new plant designers and plant upgrade designers have chosen many of the components shown in Table 1.3 to represent group compounds meeting the same family criteria Each grouping may have hundreds of discrete identifiable compounds;... characterization or assay-type hydrocarbon analysis Molecular weight is indeed a must for solving any fluidtransport design problem It, together with the subject fluid’s boiling point temperature, is the most important data to have or determine I propose that molecular weight can be determined by means of two methods Table 1.3 is again the first method proposed If your component is not specifically listed... requests, I have been handed a document used for the design of the refinery that was at least 15 to 20 years out of date with current operations While being handed these archaic wonders, I have been told, “We don’t get the ASTM test you requested from our lab, and they don’t get the proper samples to run the test you requested.” I have been even further moved by the fact that these laboratory marvels didn’t... petroleum industry has defined the many components making up crude oil and derived products simply by defining boiling range cuts Each crude oil cut is generally held to a 20°F or less boiling range increment of the total crude oil sample or the crude oil product sample Each of these boiling ranges is defined by a pseudocomponent This is not a true single component, but rather a mixture of a type of components... components Each grouped pseudocomponent mixture is treated throughout calculation evaluations as a single component These pseudocomponents thus become the key database defining all petroleum processing equipment and processing technologies There are two principal types of crude oil boiling point analysis These are the American Standard Testing Method (ASTM) and true boiling point (TBP) test procedures... construction (EPC) firms, and in each one I had very limited access to these high-priced simulation programs that do almost every calculation imaginable and a few more on top of that As a practicing process design engineer, I can remember more times I needed these simulation programs on my computer and didn’t have one, than I can remember having one when I needed it Seems these companies always have a . the Terms of Use as given at the website. The Database Industrial Chemical Process Design is indeed a toolkit offering the user practical process engineering. Having covered the difficulties of. grav- ity at any temperature by applying Fig. 1.2. Keep in mind that liquid gravities are always calculated by dividing the known density of the liquid at a certain temperature by water at 60°F or 62.4. subject temper- ature of the liquid by the density of water referenced to 60°F. With sp gr so defined, we can subsequently convert cP to cSt or cSt to cP by this simple equation. Thus the conversion