Loose Leaf For Introduction To Chemical Engineering Thermodynamics
Loose Leaf For Introduction To Chemical Engineering Thermodynamics
8th Edition
ISBN: 9781259878084
Author: Smith Termodinamica En Ingenieria Quimica, J.m.; Van Ness, Hendrick C; Abbott, Michael; Swihart, Mark
Publisher: McGraw-Hill Education
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Chapter 5, Problem 5.37P

(a)

Interpretation Introduction

Interpretation:

Develop a simplified form of the general steady-state entropy balance for single-pipe heat exchanger and justify any assumptions made.

Concept Introduction:

For a steady state flow process, the general entropy balance for an open system is defined as:

Δ(Sm)fsj Q jTσ,j=SG0   .....(1)

Where SG is the rate of entropy generation, Qj is the rate of heat transfer to a particular part of the control surface be associated with Tσ,j temperature in surroundings. Δ(Sm)fs is the net rate of change of entropy in flowing stream.

(b)

Interpretation Introduction

Interpretation:

Develop a simplified form of the general steady-state entropy balance for double-pipe heat exchanger and justify any assumptions made.

Concept Introduction:

For a steady state flow process, the general entropy balance for an open system is defined as:

Δ(Sm)fsj Q jTσ,j=SG0   .....(1)

Where SG is the rate of entropy generation, Qj is the rate of heat transfer to a particular part of the control surface be associated with Tσ,j temperature in surroundings. Δ(Sm)fs is the net rate of change of entropy in flowing stream.

(c)

Interpretation Introduction

Interpretation:

Develop a simplified form of the general steady-state entropy balance for pump and justify any assumptions made.

Concept Introduction:

For a steady state flow process, the general entropy balance for an open system is defined as:

Δ(Sm)fsj Q jTσ,j=SG0   .....(1)

Where SG is the rate of entropy generation, Qj is the rate of heat transfer to a particular part of the control surface be associated with Tσ,j temperature in surroundings. Δ(Sm)fs is the net rate of change of entropy in flowing stream.

(d)

Interpretation Introduction

Interpretation:

Develop a simplified form of the general steady-state entropy balance for gas compressor and justify any assumptions made.

Concept Introduction:

For a steady state flow process, the general entropy balance for an open system is defined as:

Δ(Sm)fsj Q jTσ,j=SG0   .....(1)

Where SG is the rate of entropy generation, Qj is the rate of heat transfer to a particular part of the control surface be associated with Tσ,j temperature in surroundings. Δ(Sm)fs is the net rate of change of entropy in flowing stream.

(e)

Interpretation Introduction

Interpretation:

Develop a simplified form of the general steady-state entropy balance for gas turbine and justify any assumptions made.

Concept Introduction:

For a steady state flow process, the general entropy balance for an open system is defined as:

Δ(Sm)fsj Q jTσ,j=SG0   .....(1)

Where SG is the rate of entropy generation, Qj is the rate of heat transfer to a particular part of the control surface be associated with Tσ,j temperature in surroundings. Δ(Sm)fs is the net rate of change of entropy in flowing stream.

(f)

Interpretation Introduction

Interpretation:

Develop a simplified form of the general steady-state entropy balance for Throttle valve and justify any assumptions made.

Concept Introduction:

For a steady state flow process, the general entropy balance for an open system is defined as:

Δ(Sm)fsj Q jTσ,j=SG0   .....(1)

Where SG is the rate of entropy generation, Qj is the rate of heat transfer to a particular part of the control surface be associated with Tσ,j temperature in surroundings. Δ(Sm)fs is the net rate of change of entropy in flowing stream.

(f)

Interpretation Introduction

Interpretation:

Develop a simplified form of the general steady-state entropy balance for nozzles and justify any assumptions made.

Concept Introduction:

For a steady state flow process, the general entropy balance for an open system is defined as:

Δ(Sm)fsj Q jTσ,j=SG0   .....(1)

Where SGis the rate of entropy generation is, Qj is the rate of heat transfer to a particular part of the control surface being associated with Tσ,j temperature in surroundings. Δ(Sm)fs is the net rate of change of entropy in flowing stream.

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For each set of measurements below, calculate the Grubbs statistic, G, look up the appropriate critical value of G from Table 4.6, and determine whether the Grubbs test supports discarding the first value in the list at the 95% level of confidence. a) 106.0, 165.0, 167.5, 170.5, 163.5, 170.7 (Geale -2.028; Gerit 1.822; yes, the Grubbs test supports discarding 106.0) b) 214.8, 263.0, 229.9, 236.9, 221.8, 230.8, 241.1 c) 357.0, 309.3, 304.9, 314.8, 305.8, 295.3, 284.7, 299.5 TABLE 4-6 Critical values of G for rejection of outlier Number of observations otsulsve os Tenos nagsibarito G to buboxy (95% confidence) 456 1.463 1.672 1.822 7 1.938 8 upa 2.032 9 2.110 10 2.176 - 1 12 15 20 11 2.234 2.285 2.409 2.557
#1 A irreversible isothermal gas-phase isomerization reaction is given as: AB. This reaction is conducted in a 400L batch reactor and 100 mol of A (NAD = 100 mol) is charged into this reactor. The rate of reaction is determined as a function of the conversion of reactant A and the results are given below. The temperature was constant at 500K and the total pressure was constant at 830 kPa. The entering number of moles of species A is 100 mol. Calculate the time necessary to achieve 80% conversion. 0 0.1 0.2 0.4 -TA (mol/m³.s) 0.45 0.37 0.3 0.195 0.6 0.113 0.7 0.079 0.8 0.05
#3 A irreversible isothermal liquid-phase reaction is given as: A → B is conducted in continuous flow systems. The rate of reaction is determined as a function of the conversion of reactant A and the results are given below. The temperature was constant at 500K. The entering molar flow rate of A is 0.4 mol/min. a) If this reaction is conducted in two CSTRS in series. Calculate the required reactor volume of each CSTRS if conversion X₁ = 0.4 and conversion X2 = 0.8. b) If this reaction is conducted in two PFRS in series. Calculate the required reactor volume of each PFRS if conversion X₁ = 0.4 and conversion X2 = 0.8. c) If this reaction is conducted in a PFR followed by a CSTR. Calculate the required reactor volume of PFR if conversion X₁ = 0.4 and of CSTR if conversion X2 = 0.8. X -A (mol/L.min) 0 0.1 0.2 0.4 0.6 0.7 0.8 0.45 0.37 0.3 0.195 0.113 0.079 0.05
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