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. vii ("About the Authors"), Line 1. "...has authored or coauthored well over..." (not over well)

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

• p. 9, Eq. (2.2-2). (10 millimeters per centimeter) (not milimeters)

• p. 12. 1 newton (N) = 1 kg-m/s²
  1 dyne = 1 g-cm/s²

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

• p. 17, 2nd line below Eq. (2.5-1). The last item in the parentheses should be 70.2% (not 73.2%).

• 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. 20, 3rd line below Week-Y table. Insert an overline above the second Y in the parentheses (Y < Ybar + 3s_Y).

• 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. 37, Prob. 2.33. In the line below the plot, T₂ = 120 (change from 160).

• p. 51, Eq. (3.3-8). First x_i should be x₁

• p. 55, Example 3.4-1, Line 3: "...assuming that g = 9.807 m/s² and noting..." (not 9.807 N/kg)

• 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. 69, Prob. 3.23, Line 2. "...700. kg/h..." (Insert decimal point after 700 to indicate 3 significant figures)

• p. 75, continuation of Prob. 3.42. In figure, replace two horizontal dimension lines (one below "500 cm," the other above "R") with a single dimension line centered between them. The 500 cm and R arrows should both extend to this single mark. Replace Part (a) with the following:

  (a) When the toluene level in the tank is 150 cm below the top (h=150 cm), the manometer fluid level in the open arm is level with the point where the manometer connects to the tank. What manometer reading, R(cm), would be observed if the manometer fluid is (i) mercury, (ii) water? Which manometer fluid would you use, and why?

• 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. 77, Prob. 3.49e. Kelvin degrees

• p. 77, Prob. 3.50.

  -- After the first sentence, add "An oversimplified diagram follows."
  -- The first sentence of Part (a) should read "Derive the linear equation for V(mV) in terms of T(^oC)."

• p. 92, 6th line from bottom. "The three remaining unknowns (n₁, n₃, and y)"...

• p. 94, Example 4.3-2. In the flowchart, delete 100.0 mol from the labeling for the bottom stream. (The correct value is 50.0, but the label is superfluous.)

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

• p. 100, first line after the first flow chart. "There are six unknowns on the chart--..."

• p. 101, bulleted H₂O balance: Interchange the + and the = (so that 0.100n₁ = n₂ + n₅)

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

• p. 106, analysis of Unit 1: Determine m₁ and x₁ (not m₂ and x₂)

• p. 107, Line 6: x₁ = 0.233 kg A/kg (not kg/h)

• 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. 116, section title. 4.6 Chemical Reaction Stoichiometry

• 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

• p. 120, Item 5 near the top of the page. "...to a point where 60 kmol is left,..." (not 60 mol)

• p. 122, Example 4.6-2, 2^nd paragraph: "Suppose the feed...2.00 mol of H₂O, and no..."
  

• p. 122, Line 8 from bottom: Numerator is y_CO2 y_H2 (not y_N2)

• p. 128, flow chart in Test Yourself. Label the feed stream 100 mol/s (not mols), and enclose the units of the output stream variables in parentheses.

• p. 132, Lines 7 and 8 (G_H2O,1...): Change Reaction 2 to Reaction 1 (once on each line)

• p. 137. In the first line after "Propane balance about mixing point," the boxed solution should be n₁ = 995 (not n₁₀).

• p. 140, last line. Change "1 mol CH₃OH generated" to "1 mol H₂O generated."

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

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

• p. 156, Prob. 4.2(b). What would you expect the reactant concentration C_A to equal...

• p. 157,
  Prob. 4.4(e), Line 2: Delete the dot above n(mol mixture)
  Prob. 4.6(b). Change "mole fractions" to "mass fractions" on Lines 1 and 3.

• p. 160, Prob. 4.15(d). Change "part (b)" to "part (c)" (two on Line 2 and one on Line 5)

• p. 165, Prob. 4.28. At the lower right of the flowchart, change the mole fraction of C to 0.430 g C/g.

• p. 166, Prob. 4.31.
  In the paragraph below the flowchart, 6th line down, replace "a fraction" with "45%".
  Part (c) should read 
  Calculate the molar amounts of the overhead and bottoms products, the mole fraction of benzene in the bottoms product, and the percentage recovery of toluene in the bottoms product (100 x moles toluene recovered/mole toluene in feed).

• p. 167, Prob. 4.33. Change species name "A" to Cr in flow chart (2 occurrences), Part (b) (two occurrences), and Part (c)(one occurrence). On flow chart, change label of overhead product stream to m₄ (kg Cr/h) [no water]

• 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 2: "The washing removes 95% of the dirt in the dirty shirts."
  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. 4.50. Part (b) should read

  "Take a basis of 100 mol C₂H₅Cl produced. Assume that the feed contains only ethane and chlorine and that all of the chlorine is consumed and do a degree-of-freedom analysis based on atomic species balances."

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

• p. 176, Prob. 4.54. In (d), implement Newton-Raphson procedure of Part (c)

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

• p. 177, Prob. 4.56(c). Revise as follows.

  The single-pass conversion in the reactor, X_sp, affects the costs of the reactor (C_r) and the separation process and recycle line (C_s). What effect would you expect an increased X_sp to have on each of these costs for a fixed formaldehyde production rate? (Hint: To get a 100% single-pass conversion you would need an infinitely large reactor, and lowering the single-pass conversion leads to a need to process greater amounts of fluid through both process units and the recycle line.) What would you expect a plot of (C_r + C_s) versus X_sp to look like? What does the design specification X_sp = 60% probably represent?

• p. 179, Line 1. "(a) For a basis of 100 mol fresh feed/h, calculate the production rate...."

• p. 182, Prob. 4.65. "Five liters...burned with 4000 gram-moles of air."

• p. 182, Prob. 4.67. Change all mol to kmol in Parts (b) and (c).

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

• p. 190. Change Equation 5.2-2 to Equation 5.1-2 in Lines 2 and 4 below the figure caption.

• 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. 212, Solution, Reduced Conditions: P_r' = 800 atm/24.0 atm = 33.3

• p. 215, Prob. 5.4d
  2^nd line. "...x_c = 0.0, 0.05, 0.10,..."
  3^rd line. "...(p_c = 2300, p_l = 1200,...) (not 300)

• 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. 223, Prob. 5.38.
  Line 4: ...pressure of 32.0 atm. The reactor temperature is raised to 235^oC and held constant thereafter until the reaction is complete. The propylene conversion at the beginning of the isothermal period is 53.2%. You may assume ideal gas...
  Part (a): What is the final reactor pressure?
  Part (b): What is the percentage conversion of propylene when P=35.1 atm?
  Part (c): Construct a graph of pressure versus fractional conversion of propylene covering the isothermal period of operation. Use the graph to confirm...

• 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. 224, Prob. 5.42, last sentence: (Assume the Cl₂ is completely consumed in the reaction Cl₂ + 2NaOH --> NaCl + NaOCl + H₂O.)

• p. 225, Prob. 5.45, Line 2: the balance noncombustible inerts.

• p. 226, Prob. 5.48(a), Line 3. "An FeS₂ oxidation of 85% is obtained, with 40% of the FeS₂ converted forming sulfur dioxide..."

• 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)
  - First bullet— P=1000 kPa, 5000 kPa, and 10,000 kPa

• 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. 232, Prob. 5.63, table entry. V_SRK = 2.1125

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

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

• p. 260, next-to-last paragraph ["1. Equation 6.4-4 may be written..."]: Change T_dp to T_bp (three occurrences in equation and two more in the rest of the paragraph)

• 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. 284, Prob. 6.21, first line. Change octane to toluene.

• p. 284, Prob. 6.23(b), last line. "...gas streams leaving and entering the condenser." (not the compressor).

• 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:
  -- Paragraph after 4th stoichiometric equation. Saturated ammonia vapor...is mixed with a stoichiometric quantity of air, and the combined stream...
  -- 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. 290, Prob. 6.43, first paragraph. ...liquid density is 0.9534 g/mL (change from .9420)

• p. 294, Prob. 6.61c. In first paragraph, add "...overhead product (or distillate)." In Part c, change distillate to overhead product.

• 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. 6.65.
  Part (b), second sentence: "Determine the mole fractions of benzene in the vapor and liquid phases and the ratio (total moles in vapor/total moles in liquid) at this point."
  Part (c): "At what temperature does the last bubble of vapor condense? What is its composition?"

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

• p. 300, Prob. 6.70, Line 1: Change "methyl alcohol" to "methanol" and change "n-propyl alcohol" to "1-propanol"

• p. 300, Prob. 6.71, Line 4. "...and the combined stream is heated and vaporized, entering the reactor at 280^oC. Gases leaving the reactor..."

• p. 301, Prob. 6.72c. "...37 lb_m TEG/lb_m water absorbed in the column."

• 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. 309, Prob. 6.101, define &nu as % removal of color/[mass of carbon/mass of dissolved sucrose]

• 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. 331, Example 7.6-2
  
  Line 1: Change "gas" to "liquid", and change 250 K to 200 K
  Last line of problem statement: Change "ideal gas behavior" to "that mixture component enthalpies are those of the pure components"

• p. 332, conclusion of Example 7.6-2
  
  Outlet stream on flow chart: Change 250 K to 200 K
  Next-to-last line of example: Change 973.3 to 434.5, and change 237.0 to 130.2
  Last line of example: Change 478 to 112 (3 such changes)

• p. 334, first boxed equation (7.7-2). The m on the right-hand side should have a dot over it.

• p. 337, example solution. The first line next to the vertical arrow should read
  "W_s = 1.00 MW = 1.00x10⁶ N-m/s (convince yourself)" (not 10⁵)
  In expression for (ΔP/ρ) next to vertical arrow, delete the conversion factor (1 N)/(1 kg-m/s²)

• 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."

• pp. 341-355, odd pages. The heading at the top right should be Problems (not Summary)

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

• p. 348, Prob. 7.33.

  -- In Line 2, delete "after expanding adiabatically."
  -- Part (a) should read "If the exiting stream were wet steam at 5 bar, what would its temperature be?" -- Part (b) should read "How much energy is transferred to or from the turbine (state which). (Neglect...)
  -- In the last variable in Part (b), there should be a dot over the E and the subscript should be k (not R).

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

• p. 351, Prob. 7.48, Line 4: Delete "ΔH = 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. 366, Test Yourself, 1(a): ...--> H₂O (l, 1200 atm)

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

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

• p. 383, flowchart for Ex. 8.4-4. The inlet stream should be labeled 1 mol, 0.500 mol B/mol, 0.500 mol T/mol

• 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. 397, 2nd line from bottom: Denominator of third factor should be 36.5 kg HCl (not 35.6). The calculated value of n is ok.

• p. 398, 2nd line from bottom: Last factor should be (2.178 kJ/mol HCl) (not 21.78)

• p. 400, top line. 0.40 lb_mH₂SO₄ = 4.08x10^-3 lb-mole, 0.60 lb_mH₂O = 3.33x10^-2 lb-mole
  In expression for ΔH₂, r = 8.2 lb-mole H₂O/lb-mole H₂SO₄ (not 1.5 lb_m H₂O/lb-mole H₂SO₄)
  In line below, the heat of mixing from Table B.11 is -279 Btu/lb_m (not +162).
  Boxed solution: Change -57 to -56 Btu/lb_m

• p. 402, graph near bottom of page. Proceeding from top to bottom, the three temperatures shown in the figure should be 100^oF (not ^oC), 150^oF (not ^oC), and 60^oF (not 50^oC)

• 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. 413, Prob. 8.22(c), Line 2. ...volumetric flow rate (m³/s) (not /h)

• p. 418, Prob. 8.50, Line 4. ...condensing 60% of the hexane in the feed. (not 80%)

• 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. 430, Line 10 from top: "Pure water at 20^oC is fed to the top of the column." (not 30^oC)

• p. 446, reaction path diagram: The reactants are C + 1/2 O₂... (not CO + 1/2 O₂...)

• p. 452, Step 4. The heat of formation of propane is -103.8 kJ/mol (not 1003.8)

• 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 and change -1134 to -1477
  In the last line of the example, T_ad = 185^oC (not 145)

• p. 459, bottom three lines. n₁ = 92.0 (not 42.3), n₂ = 58.0 (not 107.7), n₃ = 43.0 (not 92.7)

• p. 460, Line 2. Replace 42.3 with 92.0, and replace 0.687 with 0.319.

• 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 (ΔH_f^o)_NaOH(aq)

• p. 461, flowchart for Example 9.5-6. The wrong flowchart was inserted in the example. The three streams should be labeled as follows:

  Input stream 1: 1000 g 10% sulfuric acid, 0.100 g H₂SO₄/g, 0.900 g H₂O/g, 40^oC
  Input stream 2: m₁(g) 20% sodium hydroxide, 0.200 g NaOH/g, 0.800 g H₂O/g, 25^oC
  Output stream: m₂ (g Na₂SO₄), m₃ (g H₂O), 35^oC

• 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. 9.6. In Part (a), delete the coefficient 2 before CH₃OH(l).

• 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. 478, Prob. 9.12, Line 5. "...in a ratio 8.00 mol O₂/mol SiH₄, enters..." (not 10.00 mol O₂)

• 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. 491, Prob. 9.36, enthalpy table. (H_in)_CH4 = 41.65 kJ/mol (not 116.5)

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

  p. 493, Prob. 9.38(c). Change -1576 to -1510 kJ/kg

  p. 494, Prob. 9.44(b). "Estimate the final temperature if the reactor of Part (a) is adiabatic and the product solution contains 1.00 mole% ammonium sulfate. Take the heat capacity of the solution to be that of pure liquid water [4.184 kJ/(kg ^oC)]."

  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. 516, 6th line from bottom: "...containing all of the hydrogen and 1% of the isobutane..." (not 10%)

  p. 519, fifth from last row of spreadsheet cell formulas: "F17, F18,...,H10, H11, K9, K10, K11 = specific enthalpies of A, B, and C..."

  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.
  3rd of five equations in middle of page: ln(13,400-74.9T) = -74.9t + ln(8530)
  Sentence above graph: "If you evaluate T....values of t(s), a plot..."
  Abscissa of graph: t(s)
  Last sentence on page: "It takes 3.8 seconds for the temperature to reach 178^oF,..."

  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. 592. delete hyphen between gas and shift in 5^th line from bottom.

  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. 630, Table B.1. For cyclohexane gas, ΔH_f^o = -123.1 kJ/mol (not +123.1).

  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. 633, Table B.1: Molecular formulas for isopropyl alcohol and n-propyl alcohol should each be C₃H₇OH (not C₃H₅OH)

  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. Change "Methy alcohol" to "Methyl alcohol."

  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. 648, Table B.6. For P=86 bar, H(steam) = 2750.9 (not 2705.9)

  p. 651. Last pressure in steam table B.7 should be 1000

  p. 653, Table B.10. In the units for C_pa, insert the degree sign before C [J/(g-atom ^oC)]

  p. 655, TY on p. 29, Item 1(d): y² = 3 + ... (not y³)

  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. 657, TY on p. 193, Item 2, Line 2: Change 11 to 22.

  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)
  3(c)   p_H2O* = y_H2OP₀ (not y_H2O/P₀)

  pp. 659-663.
  Starting with p. 314, all Test Yourself page numbers with the exception of 317, 365, and 367 should be increased by 2 (p. 314 should be p. 316,..., p. 624 should be p. 626)
  p. 659. Change p. 317 to p. 318.
  p. 660. Change p. 365 to p. 368. Change p. 367 to p. 371

  p. 660, TY on p. 357 (when corrected, p. 359): H_hat = -2751 kJ/kg. U_hat = -2489 kJ/kg. (not -2751.1)

  p. 661, TY on p. 443 (when corrected, p. 445), Question 5, last line: Change the + before the first summation to an =.

  p. 663, TY on p. 616 (when corrected, 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. 2.14(b).  0.135 m/s²

• 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. 3.12.  Replace (a) with (b)

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

• Prob. 4.20(a).  1.2x10^-3 mol H₂O(v)/mol (not 10^-5)

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

• Prob. 4.50(c).  0.877 (not 0.875)

• Prob. 5.10.  165 m/s (not 134)

• Prob. 5.14(a).  880 cm³/s

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

• Prob. 5.26(b).  3595 mol diluting air/s

• Prob. 5.46(a).  4.08 x 10⁵ L gas/min (not 7.98)

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

• Prob. 5.50.  846 SCMH recycled

• Prob. 5.54.  49.4 kmol/h, 26% H₂, 53% CH₃OH

• Prob. 5.62.  37.4 lb_m
• Prob. 5.76.  126 ft³/min

• Prob. 6.16.  5.04x10⁴ ft³/m

• 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. 6.60(d).  0.39 m

• Prob. 6.72(c).  0.19 lb-mole H₂O/lb-mole

• Prob. 7.18(c).  ΔE_p = -W_s, W_s > 0 . (There are dots over E and W.)

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

• Prob. 7.42(a).  1.82x10⁴ cal

• Prob. 8.12(c).  Total daily cost = $4.72 (not $2.89)

• Prob. 8.22(c).  3.41 m³/s

• Prob. 8.24(c).  0.400 m³ steam/m³ propane (not 3.06)

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

• Prob. 8.30(b).  290 kW (not 423 kW)

• Prob. 8.32(a).  732^oC (not 792)

• Prob. 8.38.  -1.90 x 10⁴ kW (not -8890)

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

• Prob. 8.56(b).  163 kg/h additional steam (not 133)

• 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).  -5068 kJ/mol (not -5090)

• 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. 9.26(c).  -279 kW (process), -265 kW (reactor)

• 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)