Here is is a list of typos and plain old dumb mistakes that I made on the original first edition of Separation Process Essentials. They are bound to be legion so I will appreciate your help. If you see something, say something - firstname.lastname@example.org.
Page 10, Figure 17a. The figure was changed after the text was written so the tray numbers are not identified. You can probably figure this out.
Page 26, Table 2.1. Since I am demonstrating table formatting, I would have centered the first column. But the editor left justified them. Oh, well!
Page 39, Text uses "species" as both singular and plural in one paragraph. Can that be correct? Yes, it is. “Species” is both singular and plural.
Page 49, 4th line from bottom. Should be "... these points, that is the operating line ..." Funny how a comma can change the meaning of a sentence.
Page 59, middle of part c, the text says "Let’s choose the feed liquid …". This is not an error but could be confusing. Change to "Let’s choose the feed conditions …"
Page 61, 2/3 from top of page, the equation for HV should have vapor compositions yB=0.467 and yT=0.533 (see Figure 4.1).
Page 64, 2nd line from top, add space between L and xT for consistency.
Page 69, after 2nd equation, change “Adiabatic Flash/Flash Drum” to “Adiabatic Flash/1-Stage”] to match spreadsheet.
Page 71, at end of 2nd paragraph, remove italics from Excel “NIST”.
Page 83, Table 5.1, y1=0.495 for 2-stage, V1=66.7, R=1 (not R=0).
Page 96, bottom of page, missing shading on 2nd table. Shade all Condenser/split point cells, V1, and y1.
Page 112, top paragraph, drop the "a" in "... produces a 65 mol/s ..."
Page 113, section 7.5.1, delete the 2nd “Go ahead” as unnecessary.
Page 133, on Figure 9.1, left justify feed stream flow rates and compositions. Use V”, V’, V, L”, L’, L instead of subscripted flow rates.
Page 139, bottom table is missing a parenthesis on units for x. It is the same for top of page 140. Note that this is just a continuation of graph on page 139.
Page 140, Delta at bottom of page should equal zero, not -0.022. Page 146, add “R = 1.87” to caption of Figure 9.8.
Page 148, Figure 9.10, label for D should be empty and xD=0.75.
Page 151, in part d, change “Open Steam/MT” to “Open Steam/Operating Lines” to match spreadsheet.
Page 151, in part d, change "Open Steam/Op Lines” to “Open Steam/MT (Op Lines)” to match spreadsheet.
Page 152, in part d, change “Open Steam/MT” to “Open Steam/Operating Lines” to match spreadsheet.
Page 152, in part d, change "Open Steam/DIY” to “Open Steam/Lewis DIY” to match spreadsheet.
Page 159, note that we treat the side stream like a negative feed. Tray 4 has a feed of -5 mol/s. The side stream composition is calculated by a benzene mole balance.
Page 167, in part c, change “… Bubble point: P = KB xDB + …” to “... Bubble point: 1 = KB xDB + …”]
Note that I accidently switch to BTX (benzene, toluene, xylene) notation but the actual results are all correct for BHO.
Page 169, Figure 10.5 legend should read "BHO" not "BTO".
Page 207, in part c, change "Example 12.1" to "Example 12.2".
Page 219, add “Let’s try the bottom stage with the process specification applied there.” right after the first paragraph.
Page 219, last line should be L'/G' instead of Li/Gi.
Pages 224, in part c, the K value includes the activity coefficient that is calculated using the Wilson equation. See “Excel Stripper/7-Stage”.
Pages 227-245, the spreadsheet links for this chapter may be messed up. As of this writing, I am trying to sort this out. I believe that "Absorber Graphical" works just fine and "Stripper Graphical" is a dead link. The names in the chapter don't match.
Pages 236-7, bottom of 236 and top of 237, the molar flows are in units mol/s.
Page 245, equation should read Y = (L’/G’)X + Y1 – (L’/G’)X0]. Note that it was split and the subscripts left off.
Pages 247-9, I didn’t specify a problem. Use the specifications in Example 15.1 on page 250.
Page 280, I should have explained extract, raffinate, and plait point better. Imagine that some water (diluent) is contaminated with acetone (solute) that is removed by mixing with chloroform (solvent). The two liquid phases settle out and usually contain all three components, just in different concentrations according to the equilibrium graph. The left side of the graph (either Figure 17.1 or 17.2) is the extract. It is rich in the solvent and newly extracted solute. The right side is the raffinate. It is the diluent with small amounts of solvent and solute. The solute concentration is lowered but is now contaminated with some solvent. In a mole balance, x refers to the water (diluent) composition and y refers to the acetone (solute) composition. Subscripts F, E, and R refer to the phase: feed, extract, and raffinate, respectively.
The equilibrium compositions are determined from the tie lines. The chemicals distribute between the extract and raffinate such that the ends of the tie lines represent their compositions.
Note that these equilibrium graphs are for a specific temperature. We can assume pressure has little effect on these liquid systems.
Note that the length of the tie lines decreases as more solute is present – less separation between phases. At the very top of the graph is the plait point at which the solute composition is the same in both phases.
Page 293, in 17.3 Mathematical Analysis, change "Equations of state …" to "Activity coefficient models …". On at least this instance, I refer to activity coefficient models such as the Wilson, NRTL, and UNIQUAC as "equations of state". In fact, the only equation of state that I use in the book is the modified Raoult's law. I'll track down any place I've made that slip of the pen.