15.1: Untitled Page 237

Document Outline

• University of Alabama at Huntsville
• Chapter 1 (03-14-2014).pdf
  • Chapter 1
    • Introduction
• Chapter 02 (03-14-2014).pdf
  • Chapter 2
    • Units
  • Quantity
  • Name
  • Symbol
  • Definition
  • Physical Quantity
  • Unit (Symbol)
  • Definition
    • Mass
    • Length
  • Force
  • Time
  • Pressure
  • Volume
  • Area
    • Flow Rate
    • Power
  • Temperature
    • Kinematic Viscosity
      • A matrix is a special type of array with well-defined algebraic laws for equality, addition, subtraction, and multiplication. Matrices are defined as the set of coefficients of a system of linear algebraic equations or as the coefficients of a linear coordinate transformation. A linear algebraic system of three equations is given by
• Chapter 03 (03-14-2014).pdf
  • Chapter 3
    • Conservation of Mass for
      • Single Component Systems
• Chapter 04 (03-14-2014).pdf
  • Chapter 4
    • Multicomponent Systems
      • Figure 4-7. Laminar and turbulent velocity profiles for flow in a tube
    • Generic Degrees of Freedom (A) 12
    • Generic Specifications and Constraints (B) 6
    • Particular Specifications and Constraints (C) 6
    • Stream Variables
    • Generic Degrees of Freedom (A) (N x M) + M = 12
    • Number of Independent Balance Equations
    • Particular Specifications and Constraints (C) 6
    • Generic Degrees of Freedom (A) 16
    • Particular Specifications and Constraints (C) 9
    • Stream Variables
    • Generic Degrees of Freedom (A) (N x M) + M = 16
    • Number of Independent Balance Equations
    • Particular Specifications and Constraints (C) 9
• Chapter 05 (03-17-2014).pdf
  • Chapter 5
    • Two-Phase Systems & Equilibrium Stages
• Chapter 06 (03-19-2014).pdf
  • Chapter 6
    • Stoichiometry
      • 6.1.1 Principle of stoichiometric skepticism
• Chapter 07 (03-21-2014).pdf
  • Chapter 7
    • In terms of the global net rate of production, Axiom I takes the form
      • 7.1 Multiple Reactions: Conversion, Selectivity and Yield
        • Figure 7-2. Production of cumene
          • Figure 7.1 Catalytic production of ethylene
    • Stream & Net Rate of Production Variables
    • Generic Degrees of Freedom (A) 17
    • Number of Independent Balance Equations
    • Particular Specifications and Constraints (C) 8
      • Figure 7-3. Combustion process
      • Theoretical air
        • EXAMPLE 7.2: Determination of theoretical air
        • EXAMPLE 7.3: Combustion of residual synthesis gas
    • Figure 7.3 Combustion of synthesis gas
      • 7.3 Recycle Systems
    • Figure 7-4. Catalytic reactor with recycle
    • Figure 7-5. Recycle stream in an ammonia converter
      • 7.3.1 Mixers and splitters
    • Figure 7.4. Splitter producing three streams
    • Stream Variables
    • Generic Degrees of Freedom (A) 12
    • Number of Independent Balance Equations
      • 7.3.2 Recycle and purge streams
    • Figure 7.5a. Reactor-separator with recycle
      • Figure 7.5b. Cuts for the construction of control volumes
    • Figure 7.5c. Control volumes for vinyl chloride production unit
    • Stream & Net Rate of Production Variables
    • Generic Degrees of Freedom (A) 24
    • Number of Independent Balance Equations
    • Particular Specifications and Constraints (C) 8
      • Control Volume I
      • Control Volume II
      • Control Volume I (constraints on molar flow rates)
      • Control Volume I (constraints on global net rates of production)
      • Control Volume I (global net rates of production in terms of the conversion)
      • Control Volume II (constraints on molar flow rates)
    • Figure 7.6b. Cuts for the construction of control volumes
      • Control Volume II
    • Figure 7-7. Flowsheet for the manufacture of ethyl alcohol from ethylene
    • Figure 7.7. Control volumes for sequential analysis of a recycle system
      • Control Volume I
      • Control Volume II
      • Control Volume II
      • Control Volume III
      • Control Volume II (Reactor)
      • Control Volume III (Absorber)
        • Section 7.1
          • Figure 7.1. Production of formaldehyde
          • Figure 7.3. Pyrolysis of acetone
      • For the conversion of acetone given by
        • 7-4(. Ethylene oxide can be produced by catalytic oxidation of ethane using pure oxygen. The stream leaving the reactor illustrated in Figure 7.4 contains
        • non-reacted ethane and oxygen as well as ethylene oxide, carbon monoxide, carbon dioxide, and water. A gas stream of 10 kmol/min of ethane and oxygen is fed to the catalytic reactor with the mole fraction specified by
          • Section 7.2
    • Figure 7.14. Combustion of methane
      • Figure 7.15. Combustion of two molecular species
        • Section 7.3
    • Figure 7.28. Chemical reactor with recycle stream
    • Figure 7.31. Air dryer with recycle stream
      • For the conditions given, what is the percent of excess copper? If the conversion is given by , what is ?
        • Figure 7.35. Metallic silver production
          • Section 7.4
• Chapter 08 (03-21-2014).pdf
  • Chapter 8
    • Transient Material Balances
      • Biological compounds are produced by living cells, and the design and analysis of biological reactors requires both macroscopic balance analysis and kinetic studies of the complex reactions that occur within the cells. Given essential nutrients and a suitable temperature and pH, living cells will grow and divide to increase the cell mass. Cell mass production can be achieved in a chemostat where nutrients and oxygen are supplied as illustrated in Figure 8-8.
      • Normally the system is charged with cells, and a start-up period occurs during which the cells become accustomed to the nutrients supplied in the inlet stream. Oxygen and nutrients pass through the cell walls, and biological reactions within the cells lead to cell growth and the creation of new cells. In Figure 8-8 we have illustrated the process of cell division in which a single cell (called a mother cell) divides into two daughter cells. In Figure 8-9 we have identified species A and B as substrates, which is just another word for nutrients and oxygen. Species C represents all the species that leave the cell, while species D represents all the species that remain in the cell and create cell growth. The details of the enzyme-catalyzed reactions that occur within the cells are discussed in Sec. 9.2.
      • To analyze cell growth in a chemostat, we need to know the rate at which species D is produced (Rodgers and Gibon, 2009). In reality, species D represents many chemical species which we identify explicitly as F, G, H, etc. The appropriate mass balances for these species are given by
      • 8.6 Problems
• Chapter 9 (03-21-2014).pdf
  • Chapter 9
    • Reaction Kinetics
      • In this section we have examined the concepts of global, local, and elementary stoichiometry, along with the concept of mass action kinetics. We have made use of pictures to describe both elementary stoichiometry and elementary chemical kinetics, and we have illustrated how these pictures are related to equations. The concept of local reaction equilibrium, also known as the steady-state assumption or the steady state hypothesis or the pseudo steady-state hypothesis, has been applied in order to develop a simplified rate expression for the production of ethane and nitrogen from azomethane. The resulting rate expression compares favorably with experimental observations.
      • 9.5 Problems
• Appendices (03-21-2014).pdf
  • Tin Sn 118.69
  • Argon Ar 39.948 83.8 87.3
  • Hydrogen bromide HBr 80.912 187.1 206.1
  • Hydrogen chloride HCl 36.461 159.0 188.1
  • Hydrogen cyanide CHN 27.026 688 293 259.9 298.9
  • Mercury Hg 200.59 13,546 293 234.3 630.1
  • Nitric oxide NO 30.006 109.5 121.4
  • Nitrogen dioxide NO 30.01 112.2 122.2
  • Figure D-1. Combustion of methane
• Nomenclature (03-24-2014).pdf
  • Nomenclature