Page 199 - Analysis, Synthesis and Design of Chemical Processes, Third Edition

Fortunately, we do not have to repeat the procedure illustrated in Example 7.9 in order to estimate
for every piece of equipment. This has already been done for a large number of equipment modules, and
the results are given in Appendix A.

In order to estimate bare module costs for equipment, purchased costs for the equipment at base case
conditions (ambient pressure using carbon steel) must be available along with the corresponding bare
module factor and factors to account for different operating pressures and materials of construction. These
data are made available for a variety of common gas/liquid processing equipment in Appendix A. These
data were compiled during the summer of 2001 from information obtained from manufacturers and also
from the R-Books software marketed by Richardson Engineering Services [12]. The method by which

material and pressure factors are accounted for depends on the equipment type, and these are covered in
the next section. The estimation of the bare module cost for a floating-head shell-and-tube heat exchanger
is illustrated in Example 7.10 and in subsequent examples in this chapter.

Example 7.10

Find the bare module cost of a floating-head shell-and-tube heat exchanger with a heat transfer area of
2
100 m at the end of 2006. The operating pressure of the equipment is 1.0 bar, with both shell-and-tube
sides constructed of carbon steel. The cost curve for this heat exchanger is given in Appendix A, Figure
A.5, and is repeated as Figure 7.4. It should be noted that unlike the examples shown in Figures 7.1 and
7.2, the log-log plot of cost per unit area versus area is nonlinear. In general this will be the case, and a
second order polynomial is normally used to describe this relationship.

Figure 7.4 Purchased Costs for Floating-Head Shell-and-Tube Heat Exchangers