Solution manual heat and mass transfer a practical approach 3rd edition cengel CH11

In counter-flow, the hot and cold fluids enter the heat exchanger at opposite ends and flow in opposite direction.. Regenerative heat exchangers involve the alternate passage of the hot

Chapter 11 HEAT EXCHANGERS Types of Heat Exchangers

11-1C Heat exchangers are classified according to the flow type as parallel flow, counter flow, and

cross-flow arrangement In parallel cross-flow, both the hot and cold fluids enter the heat exchanger at the same end and move in the same direction In counter-flow, the hot and cold fluids enter the heat exchanger at opposite ends and flow in opposite direction In cross-flow, the hot and cold fluid streams move

perpendicular to each other

11-2C In terms of construction type, heat exchangers are classified as compact, shell and tube and

regenerative heat exchangers Compact heat exchangers are specifically designed to obtain large heat transfer surface areas per unit volume The large surface area in compact heat exchangers is obtained by attaching closely spaced thin plate or corrugated fins to the walls separating the two fluids Shell and tube heat exchangers contain a large number of tubes packed in a shell with their axes parallel to that of the shell Regenerative heat exchangers involve the alternate passage of the hot and cold fluid streams through the same flow area In compact heat exchangers, the two fluids usually move perpendicular to each other

11-3C A heat exchanger is classified as being compact if β > 700 m2

/m3 or (200 ft2/ft3) where β is the ratio

of the heat transfer surface area to its volume which is called the area density The area density for pipe heat exchanger can not be in the order of 700 Therefore, it can not be classified as a compact heat exchanger

double-11-4C In counter-flow heat exchangers, the hot and the cold fluids move parallel to each other but both

enter the heat exchanger at opposite ends and flow in opposite direction In cross-flow heat exchangers, the two fluids usually move perpendicular to each other The cross-flow is said to be unmixed when the plate fins force the fluid to flow through a particular interfin spacing and prevent it from moving in the

transverse direction When the fluid is free to move in the transverse direction, the cross-flow is said to be mixed

11-5C In the shell and tube exchangers, baffles are commonly placed in the shell to force the shell side

fluid to flow across the shell to enhance heat transfer and to maintain uniform spacing between the tubes Baffles disrupt the flow of fluid, and an increased pumping power will be needed to maintain flow On the other hand, baffles eliminate dead spots and increase heat transfer rate

11-6C Using six-tube passes in a shell and tube heat exchanger increases the heat transfer surface area, and

the rate of heat transfer increases But it also increases the manufacturing costs

11-7C Using so many tubes increases the heat transfer surface area which in turn increases the rate of heat

transfer

11-8C Regenerative heat exchanger involves the alternate passage of the hot and cold fluid streams through

the same flow area The static type regenerative heat exchanger is basically a porous mass which has a large heat storage capacity, such as a ceramic wire mash Hot and cold fluids flow through this porous mass alternately Heat is transferred from the hot fluid to the matrix of the regenerator during the flow of the hot fluid and from the matrix to the cold fluid Thus the matrix serves as a temporary heat storage medium The dynamic type regenerator involves a rotating drum and continuous flow of the hot and cold fluid through different portions of the drum so that any portion of the drum passes periodically through the hot stream, storing heat and then through the cold stream, rejecting this stored heat Again the drum serves

as the medium to transport the heat from the hot to the cold fluid stream

The Overall Heat Transfer Coefficient

11-9C Heat is first transferred from the hot fluid to the wall by convection, through the wall by conduction

and from the wall to the cold fluid again by convection

11-10C When the wall thickness of the tube is small and the thermal conductivity of the tube material is

high, which is usually the case, the thermal resistance of the tube is negligible

11-11C The heat transfer surface areas are A i =πD1L and A o =πD2L When the thickness of inner tube

is small, it is reasonable to assume A i ≅A o ≅ A s.

11-12C No, it is not reasonable to say h i ≈h0 ≈h

11-13C When the wall thickness of the tube is small and the thermal conductivity of the tube material is

high, the thermal resistance of the tube is negligible and the inner and the outer surfaces of the tube are almost identical ( ) Then the overall heat transfer coefficient of a heat exchanger can be

determined to from U = (1/hi + 1/ho)-1

s

o A A

11-14C None

11-15C When one of the convection coefficients is much smaller than the other , and

Then we have ( ) and thus

11-16C The most common type of fouling is the precipitation of solid deposits in a fluid on the heat

transfer surfaces Another form of fouling is corrosion and other chemical fouling Heat exchangers may also be fouled by the growth of algae in warm fluids This type of fouling is called the biological fouling Fouling represents additional resistance to heat transfer and causes the rate of heat transfer in a heat exchanger to decrease, and the pressure drop to increase

11-17C The effect of fouling on a heat transfer is represented by a fouling factor R f Its effect on the heat

transfer coefficient is accounted for by introducing a thermal resistance R f /A s The fouling increases with increasing temperature and decreasing velocity

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11-18 The heat transfer coefficients and the fouling factors on tube and shell side of a heat exchanger are

given The thermal resistance and the overall heat transfer coefficients based on the inner and outer areas are to be determined

Assumptions 1 The heat transfer coefficients and the fouling factors are constant and uniform

Analysis (a) The total thermal resistance of the heat exchanger per unit length is

C/W 0.0837°

=

°+

°+

°+

°+

°

=

+++

C/W).m0002.0(m)C)(1 W/m

380

(

2

)2.1/6.1ln(

m)]

m)(1012.0([

C/W).m0005.0(m)]

m)(1012.0([C) W/m

700

(

1

12

)/ln(

ππ

π

R

A h A

R kL

D D A

fo i o i

fi i

(b) The overall heat transfer coefficient based on the inner and the

outer surface areas of the tube per length are

C W/m 238

C W/m 317

11

m)]

m)(1012.0([C/W)0837.0(

11

11

1

π

π

o o

i i

o o i i

R

11-19 EES Prob 11-18 is reconsidered The effects of pipe conductivity and heat transfer coefficients on

the thermal resistance of the heat exchanger are to be investigated

Analysis The problem is solved using EES, and the solution is given below

0.07 0.071 0.072 0.073 0.074

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11-20 A water stream is heated by a jacketted-agitated vessel, fitted with a turbine agitator The mass

flow rate of water is to be determined

Assumptions 1 Steady operating conditions exist 2 The heat exchanger is well-insulated so that heat loss

to the surroundings is negligible and thus heat transfer from the hot fluid is equal to the heat transfer to the

cold fluid 3 Changes in the kinetic and potential energies of fluid streams are negligible 4 There is no

fouling 5 Fluid properties are constant

0

kg/m8.985

C W/m

648

0

3 - 3

The specific heat of water at the average temperature of (10+54)/2=32°C is 4178 J/kg.°C (Table A-9)

Analysis We first determine the heat transfer coefficient on the inner wall of the vessel

skg/m10513.0

)kg/m8.985(m))(0.2s(60/60Re

3

3 2

-1 2

C W/m

648

)54(2211)

100(100,13

)54(2211)100()100

75 0

25 0

w w

w

w j w g o

T

T T

T T

T

T h T T h

C W/m7226)

2.89100(100,13)

100(100,

12211

11

U

From an energy balance

kg/h 1725

)54100)(

6.06.0)(

1694()1054)(

in out

m m

T UA T

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11-21 Water flows through the tubes in a boiler The overall heat transfer coefficient of this boiler based on the inner surface area is to be determined

0

/sm10268.0/

2

2 6

ν

600,130s/m10268.0

m)m/s)(0.015

.3(Re

2 6 avg

which is greater than 10,000 Therefore, the flow is turbulent

Assuming fully developed flow,

342)

58.1()600,130(023.0PrRe023

C W/m

682

0

=

]m)m)(5(0.014C)[

W/m8400(

1

m)]

C)(5 W/m

2.14(2[

)1/4.1ln(

]m)m)(5(0.01C)[

W/m324,23

(

1

12

)/ln(

1

2 2

°

°+

=++

=

=

π

ππ

i o i

i o wall i total

A h kL

D D A h R R R R

00157.0(

11

1

π

i i i

U

R

11-22 Water is flowing through the tubes in a boiler The overall heat transfer coefficient of this boiler based on the inner surface area is to be determined

coefficient and the fouling factor are constant and uniform

0

/sm10268.0/

2

2 6

ν

600,130s/m10268.0

m)m/s)(0.015

.3(Re

2 6 avg

which is greater than 10,000 Therefore, the flow is

turbulent Assuming fully developed flow,

342)

58.1()600,130(023.0PrRe023

C W/m

682

R

C/W00475

1m)

C)(5 W/m

2.14(2

)1/4.1ln(

m)]

m)(501.0([

C/W.m0005.0m)]

m)(501.0([C) W/m324,23

(

1

12

)/ln(

1

2

2

2 ,

°+

°

=

++

+

=

ππ

ππ

π

R

A h kL

D D A

R A

h

R

o o

i o i

i i i

Then,

C W/m

00475.0(

11

1

π

i i i

U

R

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11-23 EES Prob 11-21 is reconsidered The overall heat transfer coefficient based on the inner surface as a function of fouling factor is to be plotted

1200 1650 2100 2550 3000

11-24 Refrigerant-134a is cooled by water in a double-pipe heat exchanger The overall heat transfer coefficient is to be determined

conductive and its thickness is negligible 2 Both the water and refrigerant-134a flow are fully developed 3

Properties of the water and refrigerant-134a are constant

0

/sm10004.1/

kg/m998

2 6 3

ν

ρ

Analysis The hydraulic diameter for annular space is

m015.001.0025

m)01.0(m)025.0()kg/m998(

kg/s3.0

4

2 2

3 2

ρ

ρ

i o c

avg

D D

m A

m

890,10s/m10004.1

m)m/s)(0.015729

.0(Re

V

which is greater than 4000 Therefore flow is turbulent Assuming fully developed flow,

0.85)01.7()890,10(023.0PrRe023

=(85.0)m

015.0

C W/m

598

Then the overall heat transfer coefficient becomes

C W/m

=

C W/m3390

1C

W/m50001

11

1

1

2 2

o

i h

h

U

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11-25 Refrigerant-134a is cooled by water in a double-pipe heat exchanger The overall heat transfer coefficient is to be determined

conductive and its thickness is negligible 2 Both the water and refrigerant-134a flows are fully developed

3 Properties of the water and refrigerant-134a are constant 4 The limestone layer can be treated as a plain

layer since its thickness is very small relative to its diameter

Cold water

Hot R-134a Limestone

0

/sm10004.1/

kg/m998

2 6 3

ν

ρ

m015.001.0025

m)01.0(m)025.0()kg/m998(

kg/s3.0

4

2 2

3 2

ρ

ρ

i o

m A

m

890,10s/m10004.1

m)m/s)(0.015729

.0(Re

2 6 avg

which is greater than 10,000 Therefore flow is turbulent Assuming fully developed flow,

0.85)01.7()890,10(023.0PrRe023

=(85.0)m

015.0

C W/m

598

Disregarding the curvature effects, the overall heat transfer coefficient is determined to be

C W/m

=

C W/m3390

1C

W/m3.1

m002.0C W/m50001

11

1

1

2 2

limeston o

L h

U

11-26 EES Prob 11-25 is reconsidered The overall heat transfer coefficient as a function of the limestone thickness is to be plotted

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11-27E Water is cooled by air in a cross-flow heat exchanger The overall heat transfer coefficient is to be determined

conductive and its thickness is negligible 2 Both the water and air flow are fully developed 3 Properties of

the water and air are constant

3

FBtu/h.ft

388

0

2 6

1

FBtu/h.ft

01481

0

2 4

k

Water 180°F

4 ft/s

Air 80°F

1 = +

The Reynolds number of water is

360,65s/ft10825.3

ft]

/12ft/s)[0.754

(Re

V

which is greater than 10,000 Therefore the flow of water is turbulent Assuming the flow to be fully developed, the Nusselt number is determined from

222)

15.2()360,65(023.0PrRe023

FBtu/h.ft

388

/ft10697.1

ft]

12)ft/s)[3/(412

(Re

44201

7290.0/4.01

)7290.0()4420(62.03.0

000,282

Re1

Pr/4.01

PrRe62.03.0

5 / 4 8 / 5

4 / 1 3 / 2

3 / 1 5

0

5 / 4 8 / 5

4 / 1 3 / 2

3 / 1 5 0

FBtu/h.ft

01481

=

F.Btu/h.ft26.8

1F

.Btu/h.ft1378

1

11

1

1

2 2

o

i h

h

U

Analysis of Heat Exchangers

11-28C The heat exchangers usually operate for long periods of time with no change in their operating conditions, and then they can be modeled as steady-flow devices As such , the mass flow rate of each fluid remains constant and the fluid properties such as temperature and velocity at any inlet and outlet remain constant The kinetic and potential energy changes are negligible The specific heat of a fluid can be treated

as constant in a specified temperature range Axial heat conduction along the tube is negligible Finally, the outer surface of the heat exchanger is assumed to be perfectly insulated so that there is no heat loss to the surrounding medium and any heat transfer thus occurs is between the two fluids only

11-29C That relation is valid under steady operating conditions, constant specific heats, and negligible heat loss from the heat exchanger

11-30C The product of the mass flow rate and the specific heat of a fluid is called the heat capacity rate and is expressed as When the heat capacity rates of the cold and hot fluids are equal, the temperature change is the same for the two fluids in a heat exchanger That is, the temperature rise of the cold fluid is equal to the temperature drop of the hot fluid A heat capacity of infinity for a fluid in a heat exchanger is experienced during a phase-change process in a condenser or boiler

p c m

C= &

of condensation of the steam is determined from , and the total thermal resistance of the condenser is determined from

water cooling)(

= m c T

Q& & pΔsteam

)(

= m h fg

Q& &

T Q

R= /& Δ

11-32C When the heat capacity rates of the cold and hot fluids are identical, the temperature rise of the cold fluid will be equal to the temperature drop of the hot fluid

The Log Mean Temperature Difference Method

11-33C ΔTlm is called the log mean temperature difference, and is expressed as

)/ln( 1 2

2 1

T T

T T

T lm

ΔΔ

Δ

−Δ

c in

c in

T T

temperature difference ΔTlm is obtained by tracing the actual temperature profile of the fluids along the heat exchanger, and is an exact representation of the average temperature difference between the hot and cold fluids It truly reflects the exponential decay of the local temperature difference The logarithmic mean temperature difference is always less than the arithmetic mean temperature

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11-35C ΔTlm cannot be greater than both ΔT1 and ΔT2 because ΔTln is always less than or equal to ΔTm(arithmetic mean) which can not be greater than both ΔT1 and ΔT2

11-36C No, it cannot When ΔT1 is less than ΔT2 the ratio of them must be less than one and the natural logarithms of the numbers which are less than 1 are negative But the numerator is also negative in this case When ΔT1 is greater than ΔT2, we obtain positive numbers at the both numerator and denominator

11-37C In the parallel-flow heat exchangers the hot and cold fluids enter the heat exchanger at the same end, and the temperature of the hot fluid decreases and the temperature of the cold fluid increases along the heat exchanger But the temperature of the cold fluid can never exceed that of the hot fluid In case of the counter-flow heat exchangers the hot and cold fluids enter the heat exchanger from the opposite ends and the outlet temperature of the cold fluid may exceed the outlet temperature of the hot fluid

11-38C The ΔTlm will be greatest for double-pipe counter-flow heat exchangers

11-39C The factor F is called as correction factor which depends on the geometry of the heat exchanger

and the inlet and the outlet temperatures of the hot and cold fluid streams It represents how closely a heat exchanger approximates a counter-flow heat exchanger in terms of its logarithmic mean temperature

difference F cannot be greater than unity

11-40C In this case it is not practical to use the LMTD method because it requires tedious iterations Instead, the effectiveness-NTU method should be used

11-41C First heat transfer rate is determined from Q&=m&c p[T in-T out], ΔTln from

)/ln( 1 2

2 1

T T

T T

T lm

ΔΔ

Δ

−Δ

11-42 Ethylene glycol is heated in a tube while steam condenses on the outside tube surface The tube length is to be determined

to the surroundings is negligible

, c p = 2428 J/kg⋅K, k = 0.253 W/m⋅K, µ = 0.01545 kg/m⋅s, Pr = 148.5 The thermal conductivity of copper is given to be 386 W/m⋅K

Analysis The rate of heat transfer is

W560,48C)2040)(

CJ/kg

2428)(

kg/s1()

(

kg/s1

kg/m01545.0

m)m/s)(0.02)(2.870

kg/m(1109Re

1 kg/s 20ºC

5.148()4121(023.0PrRe023

C W/m

253

100110(9200)

(

9200 − 0.25 = − 0.25 = 2 °

w g

h

Let us check if the assumption for the wall temperature holds:

C5.93)

110(025.05174)30(02.0

1677

)(

)(

)(

)(

avg ,

avg ,

w

w g o o b

w i

i

w g o o b

w i

i

T T

T

T T L D h T

T L

D

h

T T A h T

T A

h

ππ

Now we assume a wall temperature of 90°C:

C W/m4350)

90110(9200)

(

9200 − 0.25 = − 0.25 = 2 °

w g

C W/m10184350

1)

386(2

)2/5.2ln(

)025.0()02.0)(

1677(

025.0

11

2

)/ln(

copper

1 2

⋅

=++

=++

=

o o

i i o o

h k

D D D D h

D U

The rate of heat transfer can be expressed as

ln

T A U

Q&= o oΔ

where the logarithmic mean temperature difference is

C58.7920

110

40110ln

)20110()40110(ln

)()(

e g

i g e g lm

T T

T T

T T T T T

Substituting, the tube length is determined to be

m 7.63

Q& o o ln 48,560 (1018)π(0.025) (79.58)

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