*ELEMENTARY PRINCIPLES OF CHEMICAL PROCESSES*

ERRATA -- 3^{rd} Edition: Printings 1-3

Last updated: 9/22/11

**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 mi
__ll__imeters per centimeter) (not milimeters) - p. 12.
1 newton (N) = 1 kg-m/s ^{2}

1 dyne = 1__g-cm__/s^{2} - p. 16, Line 3 (equation). Denominator of first fraction should be 0.
__000__478 (not 0.00478) - p. 17, 2nd line below Eq. (2.5-1). The last item in the parentheses should be 7
__0__.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}= 7__3__%. - p. 20, 3rd line below Week-Y table. Insert an overline above the second Y in the parentheses (Y < Y
__bar__+ 3s_{Y}). - p. 32, Prob. 2.15. In Line 3, add "Express
*g*in ft/s^{2}." - 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,
*T*_{2}= 1__2__0 (change from 160). - p. 51, Eq. (3.3-8). First
*x*should be_{i}*x*_{1} - p. 55, Example 3.4-1, Line 3: "...assuming that
*g*= 9.807__m/s__^{2}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__^{o}__C__and found to be 0.9940 g/cm^{3}. - 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 "H
_{2}O" 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*(^{o}C)." - p. 92, 6th line from bottom. "The three remaining unknowns (n
_{1}, n_{3}, 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 unknown
__s__on the chart--..." - p. 101, bulleted H
_{2}O balance: Interchange the + and the = (so that 0.100n_{1}= n_{2}+ n_{5}) - p. 101, Section 4.3e, Item 2(c), Line 2: Change (kg SO
_{2}/s) to (kg__H___{2}/s) - p. 106, analysis of Unit 1:
__Determine__(not*m*_{1}and*x*_{1}*m*_{2}and*x*_{2}) - p. 107, Line 6:
*x*_{1}= 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 f
__ee__d - p. 114, Line 6 from bottom:
*m*_{4}= 1470__kg__K_{2}CrO_{4}crystals/h - p. 116, section title. 4.6
__Chemical Reaction Stoichiometry__ - p. 119, 3rd paragraph:

"More generally, if__2__ξ kmol H_{2}reacts (where 2 is the stoichiometric coefficient of H_{2}), 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__H_{2}O, 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
*n*_{1}= 995 (not*n*_{10}). - p. 140, last line. Change "1 mol CH
_{3}OH generated" to "1 mol__H___{2}__O__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(mol mixture)__n__

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 0.4
__3__0 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*m*_{4}(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 C

_{2}H_{5}Cl 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
__k__mol in Parts (b) and (c). - p. 185, Prob. 4.76(a), last line. Above the arrow, change 800
^{o}C, N_{2}to 800^{o}C,__O___{2}. - 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
__4__23 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.__6__0 (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.__0__5, 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__^{o}__C 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 NH_{3}/mole__ammonia-free__H_{2}O is fed..." - p. 224, Prob. 5.42, last sentence: (Assume
__the Cl___{2}__is completely__consumed in the reaction Cl_{2}+ 2NaOH -->__NaCl + NaOCl__+ H_{2}O.) - p. 225, Prob. 5.45, Line 2: the balance
__noncombustible__inerts. - p. 226, Prob. 5.48(a), Line 3. "An FeS
_{2}oxidation of 85% is obtained, with 40%__of the FeS___{2}__converted__forming sulfur dioxide..." - p. 228, Prob. 5.51(b).

- Line 14 (begins with "K."): Change*K*x10_{pc}^{8}to*K*x10_{yc}^{8}. (The rest of the line is correct.)

- Line 15 (begins with "L."): Change the expression following the L. to (*K*_{p}P^{2}-*K*)x10_{pc}^{8}. (The rest of the line is correct)

- First bullet—*P*=1000 kPa, 500__0__kPa, and 10,000 kPa - p. 228, Prob. 5.53. In the stoichiometric equation on Line 3, change the stoichiometric coefficient of O
_{2}to__3__(not 3/2) and the molecular formula of TPA to C_{8}H_{6}O_{4}(not C_{8}H_{6}O) - 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 "SO
_{2}Balance": Change*L*_{2}(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 AgCO
_{3}to Ag_{2}CO_{3} - p. 283, Prob. 6.20: On Lines 4 and 5, change 16 psia to 16 psi
__g__. - 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% N
_{2}" and "8.6% O_{2}and". The line should read

molar composition: 6.9% CO_{2}, 2.1% CO, 0.265% C_{6}H_{14}__(+ O___{2}__and N___{2}__)__. 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 0.9
__534__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*+1 to_{i}*y*_{i}__-1__, and change*x*_{i}__-1__to*x*_{i}__+1__.

- In Part (b), add the sentence "__Assume the stage temperature is 50__^{o}__C__."

- In Part (d), Row 4 of the spreadsheet, change*y*to_{e}*y*. On the line below the spreadsheet, change_{N}*x*to_{i}*x*_{1}. - 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^{o}C. 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 G
_{2}to G_{1} - p. 302, Prob. 6.74. Change NHCO
_{3}to N__a__HCO_{3}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^{o}C." - 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 2__0__0 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 2__0__0 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 = 1.00x10^{6}N-m/s (convince yourself)" (not 10^{5})

In expression for (Δ*P*/ρ) next to vertical arrow, delete the conversion factor (1 N)/(1 kg-m/s^{2}) - p. 338, footnote. The second conversion factor should be [(1 kJ)/(
__10__^{3}__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 "Δ
*H*= 2919" - p. 352, Prob. 7.49, Line 2. "...a face area of 400 cm
^{2}..." (not cm^{3}) - p. 355, Prob. 7.54(b). In the figure, change 3.5 bar to 3.
__1__bar - p. 366, Test Yourself, 1(a): ...--> H
_{2}O (__l__, 1200 atm) - p. 367, 4 lines below Eq. (8.3-5): Delete Δ before last
*V*_{2} - 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 0.89__7__. - 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
_{m}H_{2}SO_{4}__= 4.08x10__, 0.60 lb^{-3}lb-mole_{m}H_{2}O__= 3.33x10__^{-2}lb-mole

In expression for Δ*H*_{2},*r*=__8.2 lb-mole H___{2}__O/lb-mole H___{2}__SO___{4}(not 1.5 lb_{m}H_{2}O/lb-mole H_{2}SO_{4})

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
^{o}__F__(not^{o}C), 150^{o}__F__(not^{o}C), and__60__^{o}__F__(not 50^{o}C) - p. 410, Prob. 8.2.

Part (b), Line 2: HCN(__v__, 25^{o}C,__0.80__atm) --> HCN(__v__, 100^{o}C,__0.80__atm)

Part (c), Line 2: HCN(__v__, 25^{o}C,__50__m^{3}/kmol) --> HCN(__v__, 100^{o}C,__50__m^{3}/kmol)

Part (d), Line 2: Change 1 atm to__0.80__atm. - p. 413, Prob. 8.22(c), Line 2. ...volumetric flow rate (m
^{3}/__s__) (not /h) - p. 418, Prob. 8.50, Line 4. ...condensing
__6__0% 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
__2__0^{o}C is fed to the top of the column." (not 30^{o}C) - p. 446, reaction path diagram: The reactants are
__C__+ 1/2 O_{2}... (not CO + 1/2 O_{2}...) - 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}_{C2H5OH}*dT* - 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}= 1__8__5^{o}C (not 145) - p. 459, bottom three lines.
*n*_{1}=__92.0__(not 42.3),*n*_{2}=__58.0__(not 107.7),*n*_{3}=__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 (). In the line above the equation, change "__r__*n*moles of solvent" to "moles of solvent."__r__ - p. 460, second line from bottom: Delete the parentheses and the subscript from (Δ
*H*_{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 H_{2}SO_{4}/g, 0.900 g H_{2}O/g, 40^{o}C__Input stream 2__:*m*_{1}(g) 20% sodium hydroxide, 0.200 g NaOH/g, 0.800 g H_{2}O/g, 25^{o}C__Output stream__:*m*_{2}(g Na_{2}SO_{4}),*m*_{3}(g H_{2}O), 35^{o}C - p. 463.

Line 5 below the enthalpy table (in the H_{2}SO_{4}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 CH
_{3}OH(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 O_{2}/mol SiH_{4}, enters..." (not 10.00 mol O_{2}) - 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^{o}C is fed to the reactor. The reactor operates isothermally at 400^{o}C and the reaction goes to completion.*Data:*The average heat capacity of n-heptane between 25^{o}__C and 400__^{o}__C is 0.2427 kJ/(mol -__^{ o}__C).__" - 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^{o}C)]."- 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 0.9__00__, and change 14.0 to__13.5__. On the 3^{rd}line down from Eq. (8), change the value of*n*_{8}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 m^{3}/s to 0.__0__50 m^{3}/s

-- On the first line of the solution, change*ρ*= 0.00100 kg/m^{3}to*ρ*=__1000__kg/m^{3}- 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) = -74.9__t__+ 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^{o}F,..."- 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 SCM
__H__.- 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, Δ
*H*_{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 C
_{3}H_{7}OH (not C_{3}H_{5}OH)- p. 636, Table B.2: In the formula for the heat capacity of hydrogen cyanide, change the value of
*c*x 10^{8}from 1.092 to__-1.092__. Change "Methy alcohol" to "Methy__l__alcohol."- pp. 638-9, Table B.3. Change the vapor pressure of water at 18.6
^{o}C from 16.771 to 16.__0__71, the vapor pressure at 33.4^{o}C from 33.584 to 3__8__.584, and the vapor pressure at 95.2^{o}C from 938.59 to__6__38.59- p. 641, Table B.4. Change 1-Nonane to 1-Non
__e__ne- p. 648, Table B.6. For
*P*=86 bar,*H*(steam) = 27__50__.9 (not 2705.9)- p. 651. Last pressure in steam table B.7 should be 100
__0__- p. 653, Table B.10. In the units for
*C*_{pa}, insert the degree sign before C [J/(g-atom^{o}C)]- p. 655, TY on p. 29, Item 1(d):
*y*^{2}= 3 + ... (not*y*^{3})- p. 656, TY on p. 49, Item 5: 50
__x10__^{3}__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*_{H2O}*P*_{0}(not*y*_{H2O}/*P*_{0})- 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). - Row 3: Change -16480 to -16.480, and change J/mol to

**Answers to selected problems (p. 665-668)**

- Prob. 2.8(b). 2.
__5__kg (not 2.6) - Prob. 2.14(b).
__0.135 m/s__^{2} - Prob. 2.30(d).
*xy*= 2e^{3y/x}__[can't solve explicitly for__*y*(*x*)] - Prob. 2.32(b). 1
__10__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 H_{2}O(v)/mol (not 10^{-5}) - Prob. 4.46(b).
*X*_{A}=*X*_{B}=__0.688__(not 0.496) - Prob. 4.50(c). 0.87
__7__(not 0.875) - Prob. 5.10.
__165__m/s (not 134) - Prob. 5.14(a). 88
__0__cm^{3}/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 10^{5}L gas/min (not 7.98) - Prob. 5.48(b).
*f*_{SO2}=__0.367__at 600^{o}C (not 0.602) - Prob. 5.50.
__846__SCMH recycled - Prob. 5.54. 49.
__4__kmol/h, 2__6__% H_{2}, 5__3__% CH_{3}OH - Prob. 5.62. 37.
__4__lb_{m} - Prob. 5.76.
__126__ft^{3}/min - Prob. 6.16. 5.0
__4__x10^{4}ft^{3}/m - Prob. 6.42(a). ...15.5%
__H___{2}O (not N_{2}O) - Prob. 6.52.
__86.0__^{o}C (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 H_{2}O/lb-mole - Prob. 7.18(c). Δ
*E*_{p}= -*W*_{s},*W*_{s}> 0 . (There are dots over E and W.) - Prob. 7.28(b).
__1.27 m__^{3}__/s__(not 2.09 kg/s) - Prob. 7.42(a).
__1.82__x10^{4}cal - Prob. 8.12(c). Total daily cost =
__$4.72__(not $2.89) - Prob. 8.22
__(c)__. 3.41 m^{3}/s - Prob. 8.24(c).
__0.400__m^{3}steam/m^{3}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__^{o}C (not 792) - Prob. 8.38. -
__1.90 x 10__^{4}kW (not -8890) - Prob. 8.52(a). 2.
__42__x 10^{4}kW (not 2.06) - Prob. 8.56(b). 1
__6__3 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). -0.0
__536__kW - Prob. 9.14(c). Q =
__251__kJ (not 237.3) - Prob. 9.16(
__b__) [not (c)].__1350 kW__(not 8.11x10^{4}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 O_{2}(not 9.0) - Prob. 9.46(a).
__94__^{o}C (not 94.5) - Prob. 9.62(a).
__119__% excess air (not 99%) - Prob. 9.64(b).
__2780__^{o}C (not 2871) - Prob. 9.66(a).
__1832__^{o}C (not 1672) - Prob. 9.70(a). Change 4.7x10
^{7}kJ/d to__1.38__x10^{7}kJ/d

**Index (p. 669-675)**

Antoine equation constants, __640-641__ (not 637-638)

Convergence:

Damping parameter,

Flare,

Goalseek,

Head,

Heat,

Heat capacity,

Initiator,

Least squares, method of,

Molecular weight,

Monomer,

Newton-Raphson method,

Newton's Rule,

NO

Numerical integration,

Purge stream,

Quadrature, 377,

Reforming, 492,

Regula-falsi method,

Residual,

Simpson's rule,

Specific gravity,

Specific property,

Spreadsheet, nonlinear equation,

Steam:

Successive substitution,

Synthesis gas,

Tear:

Trapezoidal rule,

Vapor pressure,

Wegstein algorithm,

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