Changes from the text are underlined.

• Inside front cover, Factors for Unit Conversions: In the "volume" category, change 220.83 imperial gallons to 219.97 imperial gallons.

• p. xxvi. Change the page number of Chapter 14 from 607 to 602.

• p. 16, Line 3 (equation). Denominator of first fraction should be 0.000478 (not 0.00478)

• p. 18, Line 4 above Figure 2.5-1 ("for example, relatively..."): Change 0.30 to 0.98 and 0.55 to 0.99. On the next line, change 50 to 169 and 7.1 to 13. On the first of the two plots [Data Set (a)], change X_max = 72% to X_max = 73%.

• p. 32, Prob. 2.15. In Line 3, add "Express g in ft/s²."

• p. 36, Prob. 2.30. Line 1 should read "...from the given information if possible."

• p. 37, Prob. 2.32, last line of data table: Change 0.170 to 0.169.

• p. 65, Prob. 3.1(c), Line 3. Insert a period after the second word ("stones"). Change the adjacent parenthetical statement to "(A stone is a unit of mass equal to 14 lb_m. It is commonly used in England as a measure of body weight, which like the numerical equivalence between  lb_m  and  lb_f  is only valid at or near sea level.)"

• p. 67, Prob. 3.12(b), Line 2: "...sample of the stream is measured at 50^oC and found to be 0.9940 g/cm³.

• p. 75, Prob. 3.43. In the figure, move "H₂O" right, so that it clearly labels the water entering the pipe and not the space above the fluid in the sealed end of the manometer.

• p. 99, Item 2 in list, Line 2: ...must be specified before all of the remaining variable values...

• p. 101, Section 4.3e, Item 2(c), Line 2: Change (kg SO₂/s) to (kg H₂/s)

• p. 108, Line 6 below flow chart: "...degree of freedom. Similarly, the first extractor has two degrees of freedom, the second extractor has one, the extract mixing point has three,...."

• p. 114, Line 1: Change fresh food to fresh feed

• p. 114, Line 6 from bottom: m₄ = 1470 kg K₂CrO₄ crystals/h

• p. 119, 3rd paragraph:
   "More generally, if 2ξ kmol H₂ reacts (where 2 is the stoichiometric coefficient of H₂), we may follow the same reasoning and write"
  1^st equation (expression for n_H2) : Change ξ to 2ξ
  2^nd equation: Change (1/2)ξ to ξ
  3^rd equation: Change (1/2)ξ to ξ

• p. 143, Line 3. Change "nitric acid" to "nitric oxide."

• p. 155, top line. Delete the bullet in front of proportion.

• p. 157, Prob. 4.6(b). Change "mole fractions" to "mass fractions" on Lines 1 and 3.

• p. 169, Prob. 4.37, Data (bottom of page).
  Item 1: Change 2 lb_m of dirt to 2.0 lb_m of dirt
  Item 4: Change 8% Whizzo to 8.0% Whizzo

• p. 171, Prob. 4.41(d), Line 3. Change "part (a)" to "part (b)."

• p. 175, Prob. 4.52, last line: Change "acid" to "aqueous hydrofluoric acid"

• p. 176, Prob. 4.55. The problem is technically correct but unnecessarily confusing. Click here for an improved version.

• p. 185, Prob. 4.76(a), last line. Above the arrow, change 800^oC, N₂ to 800^oC, O₂.

• p. 196, Line 3. Change 323 K to 423 K.

• p. 201.
  - Line before Eq. (5.3-2): Change "Truncating...yields" to "A simple approximation that uses only the second virial coefficient is"
  - Eq. (5.3-2): Change the right-hand side of the equation to 1 + (BP/RT)

• p. 202, bulleted paragraph at the top of the page. Delete everything after the first sentence ("Solution for P...closest to V_ideal.")

• p. 202, Example 5.3-1
  - last bulleted item: Equation (5.3-2) ==> P = RT/(V^-B)
  - next line: = (0.08206 L-atm/mol-K)(122.4 K)/[1.50 L/mol - (-0.113 L/mol)] = 6.23 atm
  - last line of example: Change 8.7% to 8.0%

• p. 202, Last sentence (Perry's...to 3-272): Replace with "Standard thermodynamics references (e.g., S.M. Walas, Phase Equilibria in Chemical Engineering, Butterworth, 1985) describe the BWR equation of state and give the eight constants for a number of gases."

• p. 209, Figure 5.4-2. The figure has been misdrawn, with an extra horizontal grid line between z = 0.9 and z = 1.0. The ordinate labels should not be changed, so that the curves still asymptote to z = 1.0 on the left. The resulting errors in reading the value of z for given reduced conditions are on the order of 1-3%. On the same figure, in the numerical labels on the reduced volume curves (dashed curves), the label between 3.00 and 2.40 should be 2.60 (not 2.00).

• p. 221, Footnote 14. Replace the footnote text with Hint: Monochlorobenzene is a chlorinated hydrocarbon.

• p. 223, Prob. 5.36(b), Line 2: ...values determined in Part (a). (not b)

• p. 223, Prob. 5.37. In Part (b) and in the expression for y_A in Part (c), put a dot over the m in m_A

• p. 224, Prob. 5.41(a). "One million gallons per day of alkaline wastewater containing 0.03 mole NH₃/mole ammonia-free H₂O is fed..."

• p. 228, Prob. 5.51(b).
  - Line 14 (begins with "K."): Change K_pcx10⁸ to K_ycx10⁸. (The rest of the line is correct.)
  - Line 15 (begins with "L."): Change the expression following the L. to (K_pP² - K_pc)x10⁸. (The rest of the line is correct)

• p. 228, Prob. 5.53. In the stoichiometric equation on Line 3, change the stoichiometric coefficient of O₂ to 3 (not 3/2) and the molecular formula of TPA to C₈H₆O₄ (not C₈H₆O)

• p. 230, Prob. 5.55, Line 2. Change 5.3-4 to 5.3-2

• p. 256, Line 1 under "SO₂ Balance": Change L₂(lb_m) to n_L2(lb_m) (with a dot above the n)

• p. 243, line above bottom equation (6.1-2): delete 1 r from "rearrrange"

• p. 264, Section 6.5a, Line 4: Change AgCO₃ to Ag₂CO₃

• p. 283, Prob. 6.20: On Lines 4 and 5, change 16 psia to 16 psig.

• p. 285, Prob. 6.26(b). Delete the second sentence "(At the latter temperature...essentially zero)"

• p. 287, Prob. 6.32(a): In Line 1, change "methanol entering the absorber" to "gas entering the absorber"

• p. 288, Prob. 6.37, Line 2: delete "82.1% N₂" and "8.6% O₂ and". The line should read
        molar composition: 6.9% CO₂, 2.1% CO, 0.265% C₆H₁₄ (+ O₂ and N₂). The stack gas

• p. 290, Prob. 6.42: On the flow chart, label the second unit "Cooling, hydration, and oxidation" (When calculating the amount of oxygen fed, it is important to remember that some is needed for the final stage of the process as well as in the converter.)

• p. 296, Prob. 6.64:
  - On the schematic of Stage i adjacent to the diagram of the column, change y_i+1 to y_i-1, and change x_i-1 to x_i+1.
  - In Part (b), add the sentence "Assume the stage temperature is 50^oC."
  - In Part (d), Row 4 of the spreadsheet, change y_e to y_N. On the line below the spreadsheet, change x_i to x₁.

• p. 298, Prob. 6.67(a), Line 2. In the expression for f, make it (moles of vapor produced)/(mole of liquid fed)

• p. 301, Prob. 6.73, "Data on Process Streams" to the right of the flowchart, bottom line: Change G₂ to G₁

• p. 302, Prob. 6.74. Change NHCO₃ to NaHCO₃ in Line 1 and at the beginning of Line 2.

• p. 304, Prob. 6.85, Line 3: "to 1.00 kg of the solution to raise the normal boiling point by an additional 3^oC."

• p. 318, 2nd line below Eq. (7.3-2). "initial system energy..." (not intitial)

• p. 323, Eqs. (7.4-14b) and (7.4-14c): Insert dot above m (4 occurrences)

• p. 324, figure in Example 7.4-2. The Q arrow should be pointing into the box rather than coming out of it, and there should be dots above Q and W.

• p. 338, footnote. The second conversion factor should be [(1 kJ)/(10³ N^.m)] (not [(1 kJ)/(1 N^.m/s)] )

• p. 340, Line 5 below Eq. (7.7-2): Delete the inverted question mark between "of" and "Equation."

• p. 345, Prob. 7.23. In Line 4, change 20.2 kJ to 20.2 J.

• p. 350, Prob. 7.42, Line 6 below "Stream Data" (Boilup): Change "Liquid" to "Vapor"

• p. 351, Prob. 7.48, Line 4: Delete "&rDelta;H = 2919"

• p. 352, Prob. 7.49, Line 2. "...a face area of 400 cm²..." (not cm³)

• p. 355, Prob. 7.54(b). In the figure, change 3.5 bar to 3.1 bar

• p. 367, 4 lines below Eq. (8.3-5): Delete &rDelta; before last V₂

• p. 370, line above "Calculate &rDelta;U" heading. Change kg to kJ in units of C_v

• p. 386, Fig. 8.4-2. The vertical scales on the far right of the figure are slightly misaligned and do not reflect the fact that 1 lb = 7000 grains. The scale on the left (grains moisture/lb dry air) is more accurate. The maximum error in absolute humidity on the rightmost scale (lb moisture/lb dry air) is roughly 1%.

• p. 389, boxed set of chart values toward bottom of page, value of V: Change 0.895 to 0.897.

• p. 410, Prob. 8.2.
  Part (b), Line 2: HCN(v, 25^oC, 0.80 atm) --> HCN(v, 100^oC, 0.80 atm)
  Part (c), Line 2: HCN(v, 25^oC, 50 m³/kmol) --> HCN(v, 100^oC, 50 m³/kmol)
  Part (d), Line 2: Change 1 atm to 0.80 atm.

• p. 420, Prob. 8.57(a). Change "molar" to "mass"

• p. 427, Prob. 8.66(b), Row 5 of spreadsheet: Change the values of A, B, and C for n-pentane to 6.84471, 1060.793, and 231.541, respectively.

• p. 429, Prob. 8.67, last line before statement of Part (a): Add "The Antoine equation coefficients for propane are A=7.58163, B=1133.65, C=283.26."

• p. 457. In the expression under "Calculate Inlet Enthalpy," the integrand should be (C_p)_C2H5OHdT

• p. 458, end of Example 9.5-3: In the third line from the end of the example, change 2.879 to 2.813

• p. 460. In Eq. (9.5-3), change (n) to (r). In the line above the equation, change "n moles of solvent" to "r moles of solvent."

• p. 460, second line from bottom: Delete the parentheses and the subscript from (&rDelta;H_f^o)_NaOH(aq)

• p. 463.
  Line 5 below the enthalpy table (in the H₂SO₄ calculation): change 58.9 kJ to 57.8 kJ.
  On the bottom line and 3 lines above it, change -1349 kJ/mol to -134.9 kJ/mol.
  On the bottom line, change -1375 kJ to -136 kJ

• p. 470, 4^th complete paragraph, first sentence. "There exist two values of the mole percent of fuel in a fuel-air mixture--the lower or lean flammability limit and the upper or rich flammability limit--that define a range within which self-sustaining combustion can occur. A fuel-air mixture...."

• p. 477, Prob. 9.7(d), Line 3: Change the line to read "required heat of reaction, use tabulated heats of fusion, which you should assume to be temperature-independent.")

• p. 479, Prob. 9.14, first paragraph. "Normal heptane is dehydrocyclized to toluene and hydrogen in a continuous vapor-phase reaction. Pure heptane at 400^oC is fed to the reactor. The reactor operates isothermally at 400^oC and the reaction goes to completion. Data: The average heat capacity of n-heptane between 25^oC and 400^oC is 0.2427 kJ/(mol - ^oC)."

• p. 480, Prob. 9.18.
  Line 3: "The flowchart shown below...basis of 1 mol FeO fed at 298K."
  Flow chart: There should be two separate feed streams--one for 1 mol FeO at 298K and the other for n_o mol CO(g) at T_o(K)
  Partial spreadsheet (toward bottom of p. 481):
  Row 3: Change -16480 to -16.480, and change J/mol to kJ/mol
  Row 7: Change 1520 to 1.520, 13482 to 13.482, and 11863 to 11.863

  p. 484, Prob. 9.24. In the sentence immediately after the two stoichiometric equations ("The reactions of ethylene...reaction system."), change "hydrogen" to water (two occurrences).

  p. 492, Prob. 9.38(b), Line 5: Change 51.5 to 51.37.

  p. 494, Prob. 9.45, Line 3: Change -1.2 kJ/mol to -1.17 kJ/mol

  p. 494, Prob. 9.46(a), Line 3: "...pure liquid water, the standard heat of solution of sodium sulfate is -1.17 kJ/mol, and the energy balance..."

  p. 495, Prob. 9.50, Line 4: Change 841.9 kJ/mol to 963.7 kJ/mol

  p. 495, Prob. 9.51. In Line 2, add "Assume that the pressure is low enough for all the exiting water to be vapor."

  p. 524, Eq. (8): Change 93.3% to 90%, change 0.933 to 0.900, and change 14.0 to 13.5. On the 3^rd line down from Eq. (8), change the value of n₈ from 14.0 to 13.5.

  p. 548, Example 11.2-1:
  -- On the flow chart, change the flow rate of the feed stream from 0.50 m³/s to 0.050 m³/s
  -- On the first line of the solution, change ρ = 0.00100 kg/m³ to ρ = 1000 kg/m³

  p. 550, Eq. (11.2-1): Delete "(s^-1)"

  p. 552, Example 11.2-2: On the flow chart, change the flow rates of the feed and effluent streams from 1.150 L/s to 0.150 L/s

  p. 559.
  Sentence above graph: "If you evaluate T....values of t(s), a plot..." (lower case s in parentheses, not 5)
  Last sentence on page: "It takes 3.8 seconds for the temperature to reach 178^oF,..." (delete period after "seconds")

  p. 583, Step 12: On Line 4, change "Step 8" to "Step 9"

  p. 586, Prob. 12.10, Line 1: Change "mole fraction" to "mass fraction."

  p. 587, Prob. 12.19(d), Line 3: Change 6.5-11 to 6.5-5.

  p. 588, Prob. 12.26, Line 1: Change "resin neutralizer" to "waste liquor neutralizer."

  p. 596, Prob. 13.1, Line 5: Change SCMM to SCMH.

  p. 608, Eq. (A.1-2): Insert subscript i next to x in the second summation. The term should be (y_i - ax_i - b)².

  p. 631, Table B.1. The normal boiling point of mercury should be 356.7 (not -356.9). The standard heat of combustion of liquid methanol should be -726.6 (not +726.6)

  p. 632, Table B.1. In the entry for Phosphorus(red), the 0(c) in the next-to-last column belongs to Phosphorus(white) at the top of the next page.

  p. 636, Table B.2: In the formula for the heat capacity of hydrogen cyanide, change the value of c x 10⁸ from 1.092 to -1.092

  pp. 638-9, Table B.3. Change the vapor pressure of water at 18.6^oC from 16.771 to 16.071, the vapor pressure at 33.4^oC from 33.584 to 38.584, and the vapor pressure at 95.2^oC from 938.59 to 638.59

  p. 641, Table B.4. Change 1-Nonane to 1-Nonene

  p. 656, TY on p. 49, Item 5: 50x10³ mol/h (not 50 kmol/h)

  p. 657, TY on p. 190, Item 1: On Line 3, change 200 g/s to 255 g/s.

  p. 658, TY on p. 212, Line 1: Change 5.3-4 to 5.4-3

  p. 658, TY on p. 253
  2.   200 mm Hg; 760 mm Hg... (not 600)

  p. 661, TY on p. 445, Question 5, last line: Change the + before the first summation to an =.

  p. 663, TY on p. 618: "2. A line...plot through (2, 2.3) and (2.3, 2.45)..." (not 2, 2.345).

Answers to selected problems (p. 665-668)

• Prob. 2.8(b).    2.5 kg (not 2.6)

• Prob. 2.30(d).  xy = 2e^3y/x [can't solve explicitly for y(x)]

• Prob. 2.32(b).  110 kg/h (not 109)

• Prob. 3.42(a).  h = 400 cm ==> R_water = 646 cm

• Prob. 4.46(b).  X_A = X_B = 0.688 (not 0.496)

• Prob. 4.50(c).  0.877 (not 0.875)

• Prob. 5.14(a).  880 cm³/s

• Prob. 5.24(b).  $1,747,000/month (not 1,048,000)

• Prob. 5.48(b).  f_SO2 = 0.367 at 600^oC (not 0.602)

• Prob. 6.16.  5.04x10⁴ ft³/m (not 5.07)

• Prob. 6.42(a).  ...15.5% H₂O (not N₂O)

• Prob. 6.52.  86.0^oC (not 85.85)

• Prob. 6.54(a).  P = 76 psig (not 151)

• Prob. 7.28(b).  1.27 m³/s (not 2.09 kg/s)

• Prob. 7.42(a).  1.82x10⁴ cal

• Prob. 8.26(b).  Relative humidity = 79.7% (not 51.2%)

• Prob. 8.32(a).  732^oC (not 792)

• Prob. 8.52(a).  2.42 x 10⁴ kW (not 2.06)

• Prob. 8.74(b).  2.9 tons of cooling (not 1.35)

• Prob. 9.6(a).  122.7 kJ/mol (not 245.4)

• Prob. 9.10(b).  Change -5090 kJ/mol to -5068 kJ/mol

• Prob. 9.12(c).  -0.0536 kW

• Prob. 9.14(c).  Q = 251 kJ (not 237.3)

• Prob. 9.16(b) [not (c)]. 1350 kW (not 8.11x10⁴ kJ/min)

• Prob. 9.18(c).  Q = 11.86 kJ (not 11,863)

• Prob. 9.28(b).  Delete the minus signs in front of the three heat flow rates.

• Prob. 9.30(c).  55.7 kmol recycled/h (not 55.9)

• Prob. 9.38(c).  35.4 mol O₂ (not 9.0)

• Prob. 9.46(a).  94^oC (not 94.5)

• Prob. 9.62(a).  119% excess air (not 99%)

• Prob. 9.64(b).  2780^oC (not 2871)

• Prob. 9.66(a).  1832^oC (not 1672)

• Prob. 9.70(a).  Change 4.7x10⁷ kJ/d to 1.38x10⁷ kJ/d

Index (p. 669-675)

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