BASIC PRINCIPLES AND CALCULATIONS IN CHEMICAL ENGINEERING BOOK
Basic Principles and Calculations in Chemical Engineering (8th Edition) Hardcover . His books include Chemical Process Control, Second Edition and An. Basic Principles and Calculations in Chemical Engineering: James B. Riggs David M. Himmelblau: Books - ppti.info Where those designations appear in this book, and the publisher was aware of a Basic principles and calculations in chemical engineering.
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Book Description. The Number One Guide to Chemical Engineering Principles, Techniques, Calculations, and Applications: Now Even More Current, Efficient. solutions manual basic principles and calculations in chemical engineering The authors and publisher have taken care in the preparation of this book, but. Basic Principles and Calculations in Chemical Engineering Eighth Edition .. 4 ( Open Book, 2 hours) PROBLEM 1 (25%) In the vapor-recompression evaporator .
Balances to be solved: Cu Balance: Cu overall: A sand balance around the feed mixer: A total balance around the feed mixer.: Therefore, it would be wise to condense the HCl and H2O by cooling. Perhaps the acid solution might be sold to help pay for the process. Although the problem seems to be underspecified, when you draw a diagram of the process and place the known data on it, the situation becomes clearer.
Assume the process is a steady state open one with reaction. If you use the extent of reaction, you make species balances. If the equations are independent, we can find a unique solution. After selection of a basis, the air flow is known.
Hence, this problem can be solved by direct addition and subtraction Unknowns: Total 6 Step 7: Can make C, H, O, N element balances. Element Balances: C, H, N, O Equations: Use x and y as mol: C balance: Use extent of reaction and species balances. Another equation needed for CO: Basis mol P Step 6: F, A, W all compositions known Step 7: C, H, O, N 1 extra balance Steps 8 and 9: C, H, O, inert, N2 5 Steps 8 and 9: Balances in moles: Check via C: P, x, y, z Step 7: Use the extent of reaction and species balances 5.
Basic Principles and Calculations in Chemical Engineering – Himmelblau – Book Review
Use CO2: C, H, O, N is one redundant? Element balances in out C: F, A, B, W Step 7: C, O, H, N ok Steps 8 and 9: Via algebra 2N balance: Use extent of reaction and species balances, but it is more complicated. Similarly, the other values of the moles in P would not change. The values of the pertinent components for NOx use NO1.
The sum of the components in moles would equal the total flow, hence not all of the equations that could be written would be independent, only 2 per subsystem. Total balances: In addition, 2 component balances could be written for each component for each subsystem cited above. Multiply Fi by the composition xij. Species in 1: Overall balances: Salt balance on the freezer: No reaction occurs and the process is assumed to be in the steady state.
Steps are omitted here. The balances are System: Splitter System: Stock Chest Total: This is a steady state flow process without reaction. Unknowns are: Balances are: In Out C kg mol: Step 7: C kg mol: This is a steady state process with no reaction taking place. All the compositions are known except for stream C. We can pick the overall system first to get D, and then make balances on the first or second units to get C and its composition.
For the overall system there are 4 unknowns C is excluded and 5 species balances: Overall balances kg In Out NaCl: Two of the equations are not independent: HC1 and H2SO4. Unit 2: The solution is simplified if two balances are made first not an essential step: All material balances are in kg.
Solids balance on Unit 2 and also Unit 1: Steps 6 and 7: Overall balances Total: Unknowns 5: A, B Implicit equations 2: A, D, E Balances: H, Cl, Si Steps 8 and 9: Overall system Step 6: Duct Step 6: If have separate air streams, we have 5 unknowns and can't solve.
Material and Energy Balances, Second Edition, 2nd Edition
A, B, D, E, G 4 balances: Na, C1, H, O other equations: Fe added: Unknowns 9: Mol TiO2 in slag: Mol Fe in Slag: Exit H2O from dryer: The pounds of TiO2 produced P: By reaction 3 , 0. F, P Balances: A, B Steps 8 and 9: G, R Balances: A, B or total as alternate Steps 8 and 9: B, D Balances: Total, B1, B2, S not all independent Steps 8 and 9: Total balance: Adsorber balance of U units are U: Revised compositions are in mass fractions.
H2O 0. Dried cereal H2O 0. Fresh air, Basis mol Exit air, Basis 1. KNO3 0. Compute the weight fraction composition of R.
On the basis of 1 kg of water, the saturated recycle steam contains 1. The recycle steam composition is 0. Analysis of complete process 6 streams: W, C, Balances: Either a a balance around the evaporator or b a balance around the crystallizer will do. The latter is easier since only three rather than four unknown streams are involved. Total balances on crystallizer: Single pass conversion based on H2 as the limiting reactant: Step 6: C, H, O Steps 8 and 9: Element balances C mol: O mol: Then fSP 0.
The single pass conversion for Ca AC 2 is 0. C2 H5 produced per hour Step 5: Recycle Make balance on the mixing point. Balance over separator. Mole ratio of ZnBr2 to C2H2 in final products: F2, P1, P2 Element balances: Use the extent of reaction to get the same results.
Pick the overall process as the system. The system is as shown in the diagram with recycle added. Recycle is not involved in the overall balance, hence the concentration of NO will not be affected because the extent of reaction with and without recycle remains the same. The recycle does reduce the combustion temperature, which in turn will reduce the exit concentration of NO. P 3, 0. Not all of the balances are independent: In the diagram use mol and mass percent for compositions and mol and mass for flow as specified.
F, S, W Step 7: Can make total and 3 component balances: Fermentation Product Balance: Overall System A 0. Reactor plus separator System B in out gen. Consumption accum Na 2S balance: All of it reacts. Mixing Point: In Out F C3 H8: Use stochiometry mol mol fr kg mol SO3 0.
The unknowns are the 4 exit compositions plus the extent of reaction if it is to be used. Steps 7, 8, and 9: We can use a mixture of element and species balances. Non Bz is non-benzene Step 5: P, 3miW 4 Balances: Unit 1 Steps 6 and 7: Bz, nonBz, SO2 Steps 8 and 9: Balances are in kg b.
HNO3 is 3 HNO3 is C, H, S, O, N or you can use stoichiometry and make species balances, or use the extent of reaction C: Do numbers check? The bottom stream from the distillation column and the wastewater stream from the condenser are candidates. The bottoms stream from the distillation column contains no NH3 and has the highest mass fraction of AN of any waste stream so that the entire stream could be fed to the scrubber.
The change in the scrubber feed will not affect any of the stream flows or compositions upstream of the scrubber that are connected to the scrubber, namely those associated with the reactor and the subsequent condenser, nor any downstream flows not connected to the scrubber. A sequential set of material balances can be used to get the flows and concentrations in the rest of the process.
Let x be the kg of AN entering or leaving a particular unit. The solution of these equations is in kg note the changes are quite small, hence the number of significant figures is exaggerated: CO2 Makeup 3: Reformer balance Condenser balance CO conv. Solve balances serially. Reformer balance gives stream 3 99 kgmol CH4 conv.
Stream 4: N2 is inert species: Hg absolute The simplest way to proceed, now that the data are in good order, is to apply the ideal gas law. Take as a basis, Determine the initial pressure in the O2 tank alone.
H2 O Hg Basis: Data in the diagram State 1 is before corking; state 2 is after equilibrium is reached after filling. Hg abs. Use the ideal gas law: Calculate the inlet cross-sectional area A: Calculate the inlet volumetric flow rate Q: Calculate the outlet volumetric flow rate using the ideal gas law: Calculate the outlet cross-sectional area: Calculate the outlet duct diameter: Besides inconvenience, the discharge concentration from the hood vent may be unacceptable.
Comp Mol Mol. P and all the compositions of P 5 unknowns Step 5: Gas listed in the figure Steps 6 and 7: Unknowns p final , V final ; Equations: Gas with given data Steps 6 and 7: P, F Step 7: Balances are in moles SF6: Gas, CO2 Steps 8 and 9: Balance overall on process in moles Gas: Also, assuming a leak would bring no additional CO2 into the system, the above CO2 balance calculations indicate the given analysis is probably correct.
Steady state problem with a reaction. Unknowns are the moles in P 4 plus P. You can use element balances or compound balances. The former is easier. Calculate A given the Balances kg mol In Out C: Increase 7. Including those products will have negligible effect on the N2 and CO2 produced. Base the CO2 on the emission factor value. SO2 3. Mass fraction kg MW kg mol C 0. Steady state with reaction and recycle Step 5: Select the overall system for the first balances.
Volumetric flow rates: Pick the system of the reactor plus separator, and use the data for the conversion.
Basis 10, kg 1. Mixing point: CO2 Steady state process with reaction.
Step 6, 7, 8, 9: Element balance: For other answers, look at the answer to P You can decide how much RT accuracy is needed. RK Equation: SRK Equation: Data as above: Calculate the moles of NH3: From Polymath CO2 at 81 psig and 25oC Pressure in can Solution by compressibility factor method: Use Excel to solve this cubic equation to obtain a positive, real answer.
Use the compressibility factor method. SRK equation: Use of the Pitzer ascentric factor would require a trial and error solution. It is a liquid sp. Data on gases cited in problem. To find the amount of gas in the cylinder, first find the approximate volume in the cylinder. For C2H4: MW is Si is Let T - K. Assume the number of moles does not change. Then type IA is selected because it is the cheapest. Assume a continuous process although a batch process would be acceptable and give the same results.
MW C2H4 0. G at given conditions Steps 6 and 7: Calculate G: C2H4 F 0. Steps 2, 3, and 4: Separator Bz 0.
Description du produit
Tol 0. MW kg mass fr. Tc K pc atm Bz 50 The balances in kg are only 3 are independent mass balances 1 Bz 30, 0. Using 1 , 2 , 3 , 5 , and 6 via Polymath kg mass fr.
Possible variables are: In mm Hg kPa mm Hg 2. It is a typo. Probably the number was State 1: The weights are the respective amounts of each phase. Use semi-log paper with the horizontal axis log Obtain vertical scale rules by use of steam properties at even integers for the temperature. Or you can use Antoine Equation, Appendix G, to get 2 points and draw a line between them.
Tcritical o F p critical cox chart psia pcritical psia a Acetone b Heptane c Ammonia d Ethane On logarithmic paper, set up the pressure scale on one axis.
The other axis will be a nonlinear temperature scale, which will be set up by the following method. Draw a diagonal line from the origin to the opposite corner of the graph. From the steam tables, obtain values for the vapor pressure of water at evenly spaced temperature increments.
Plot these vapor pressures along the diagonal line. Now, beginning with the first point on the diagonal, draw a line extending from that point to the temperature axis and label the intersection as the corresponding temperature for that vapor pressure. Repeat step five for every point on the diagonal line. This process will establish the temperature scale. Using the established temperature scale, plot the data for benzene and draw a line through the points.
The result from the Cox chart is that the vapor pressure for aniline at o is 22 atm. CCl3NO2 0. That means their breath can hold a bit more moisture than ours, and on that day, that extra moisture could have been just enough for condensation to occur.
It could be that it was a few degrees colder on the beach than where the observer was sited. And, as you know if you have ever experimented with seeing your breath, the bigger the volume of air, the more moisture available to condense out and so the condensed moisture was more visible. Assume the barometer is mm Hg abs. The above greatly exceeds this limit. Hg total lb mol hr Alternate solution: A mercury spill can be cleaned up reasonably effectively by dusting with sulfur, then vacuuming with a vacuum cleaner specifically designed for mercury pick-up, which prevents the escape of mercury vapor.
System is loading plus water seal, steady state, open C4 P Comp. H2O sat 2. At P, the mole fraction of water is 2. Refrigerator is system Steps 6 and 7: W2 and P; balance: H2O and air Steps 8 and 9: Basis is Mol F Step 6: W, P Step 7: The 2 answer is close to correct because of the very small amount of water.
The process is open, steady state with reaction. The first objective is to make material balances. Introductory Concepts Part II: Material Balances Chapter 3.
Material Balances Chapter 4. Material Balances without Reaction Chapter 5. Material Balances Involving Reactions Chapter 6. Gases, Vapors, and Liquids Chapter 7. Ideal and Real Gases Chapter 8. Multiphase Equilibrium Part IV: Energy Chapter 9.
Energy Balances Chapter Energy Balances: How to Account for Chemical Reaction Chapter Supplementary Material Chapter Heats of Solution and Mixing Chapter The Mechanical Energy Balance Chapter Problem Solving 4. Gases, Vapors, Liquids, and Solids 5. Energy Balances 6. Solving Simultaneous Material and Energy Balances 7. B Atomic Weights and Numbers App. C Steam Tables App.
E Heat Capacity Equations App.The total pressure is 1 atm. The bottle is weighted after the air is blown for 2 hours, 13 minutes, 47 seconds, and the decrease in weight was found to be 8. Use Excel to solve this cubic equation to obtain a positive, real answer.
ISBN 13: 9780132346603
Mixing Point: On one test of the proposal you add ten pounds of NaBr per hour for 24 hours to a sewage stream with essentially no Br— in it. Heats of Solution, Dissolution, and Mixing. FeC13 2.
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