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heat transfer cheat sheet, Cheat Sheet of Physics

Complete and schematic heat transfer equation cheat sheet

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HEAT TRANSFER EQUATION SHEET
Heat Conduction Rate Equations (Fourier's Law)
Heat Flux : 𝑞𝑥
′′=−𝑘𝑑𝑑
𝑑𝑥 𝑊
𝑚2
k
: Thermal Conductivity 𝑊
𝑚∙𝑘
Heat Rate : 𝑞𝑥= 𝑞𝑥
′′𝐴𝑐 𝑊
Ac
: Cross-Sectional Area
Heat Convection Rate Equations (Newton's Law of Cooling)
Heat Flux: 𝑞′′ =(𝑇𝑠𝑇) 𝑊
𝑚2
h
: Convection Heat Transfer Coefficient 𝑊
𝑚2∙𝐾
Heat Rate: 𝑞=ℎ𝐴𝑠(𝑇𝑠𝑇) 𝑊
As
: Surface Area 𝑚2
Heat Radiation emitted ideally by a blackbody surface has a surface emissive power: 𝐸𝑏= 𝜎 𝑇𝑠4 𝑊
𝑚2
Heat Flux emitted : 𝐸= 𝜀𝜎𝑇𝑠4 𝑊
𝑚2 where ε is the emissivity with range of 0 𝜀 1
and 𝜎= 5.67 ×10−8 𝑊
𝑚2𝐾4 is the Stefan-Boltzmann constant
Irradiation: 𝐺𝑎𝑏𝑠 = 𝛼𝐺 but we assume small body in a large enclosure with 𝜀=𝛼 so that 𝐺= 𝜀 𝜎 𝑇𝑠𝑠𝑠
4
Net Radiation heat flux from surface: 𝑞𝑠𝑎𝑑
′′ =𝑞
𝐴= 𝜀𝐸𝑏(𝑇𝑠) 𝛼𝐺= 𝜀𝜎(𝑇𝑠4 𝑇𝑠𝑠𝑠
4)
Net radiation heat exchange rate: 𝑞𝑠𝑎𝑑 = 𝜀𝜎𝐴𝑠(𝑇𝑠4 𝑇𝑠𝑠𝑠
4) where for a real surface 0≤𝜀≤1
This can ALSO be expressed as: 𝑞𝑠𝑎𝑑 = 𝑠𝐴(𝑇𝑠 𝑇𝑠𝑠𝑠) depending on the application
where 𝑠 is the radiation heat transfer coefficient which is: 𝑠= 𝜀𝜎(𝑇𝑠+ 𝑇𝑠𝑠𝑠)(𝑇𝑠2+ 𝑇𝑠𝑠𝑠
2) 𝑊
𝑚2∙𝐾
TOTAL heat transfer from a surface: 𝑞=𝑞𝑐𝑐𝑐𝑐+𝑞𝑠𝑎𝑑 =ℎ𝐴𝑠(𝑇𝑠𝑇)+𝜀𝜎𝐴𝑠(𝑇𝑠4 𝑇𝑠𝑠𝑠
4) 𝑊
Conservation of Energy (Energy Balance)
𝐸󰇗𝑖𝑐+𝐸󰇗𝑔 𝐸󰇗𝑐𝑠𝑜 = 𝐸󰇗𝑠𝑜 (Control Volume Balance) ; 𝐸󰇗𝑖𝑐 𝐸󰇗𝑐𝑠𝑜 = 0 (Control Surface Balance)
where 𝐸󰇗𝑔 is the conversion of internal energy (chemical, nuclear, electrical) to thermal or mechanical energy, and
𝐸󰇗𝑠𝑜 = 0 for steady-state conditions. If not steady-state (i.e., transient) then 𝐸󰇗𝑠𝑜 =𝜌𝜌𝑐𝑝𝑑𝑑
𝑑𝑜
Heat Equation (used to find the temperature distribution)
Heat Equation (Cartesian): 𝜕
𝜕𝑥𝑘𝜕𝑑
𝜕𝑥+ 𝜕
𝜕𝜕𝑘𝜕𝑑
𝜕𝜕 + 𝜕
𝜕𝜕𝑘𝜕𝑑
𝜕𝜕+ 𝑞󰇗=𝜌𝑐𝑝𝜕𝑑
𝜕𝑜
If 𝑘 is constant then the above simplifies to: 𝜕2𝑑
𝜕𝑥2+ 𝜕2𝑑
𝜕𝜕2+ 𝜕2𝑑
𝜕𝜕2+𝑞󰇗
𝑘=1
𝛼𝜕𝑑
𝜕𝑜 where 𝛼=𝑘
𝜌𝑐𝑝 is the thermal diffusivity
Heat Equation (Cylindrical): 1
𝑠𝜕
𝜕𝑠𝑘𝑘𝜕𝑑
𝜕𝑠+1
𝑠2𝜕
𝜕𝜕𝑘𝜕𝑑
𝜕𝜕 + 𝜕
𝜕𝜕𝑘𝜕𝑑
𝜕𝜕+ 𝑞󰇗=𝜌𝑐𝑝𝜕𝑑
𝜕𝑜
Heat Eqn. (Spherical): 1
𝑠2𝜕
𝜕𝑠𝑘𝑘2𝜕𝑑
𝜕𝑠+1
𝑠2sin𝜃2𝜕
𝜕𝜕𝑘𝜕𝑑
𝜕𝜕 + 1
𝑠2sin𝜃 𝜕
𝜕𝜃𝑘sin 𝜃𝜕𝑑
𝜕𝜃+ 𝑞󰇗=𝜌𝑐𝑝𝜕𝑑
𝜕𝑜
Thermal Circuits
Plane Wall: 𝑅𝑜,𝑐𝑐𝑐𝑑 =𝐿
𝑘𝐴 Cylinder: 𝑅𝑜,𝑐𝑐𝑐𝑑 =ln𝑟2
𝑟1
2𝜋𝑘𝐿 Sphere: 𝑅𝑜,𝑐𝑐𝑐𝑑 =
(1
r11
r2)
4𝜋𝑘
pf3
pf4
pf5
pf8
pf9
pfa
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HEAT TRANSFER EQUATION SHEET

Heat Conduction Rate Equations (Fourier's Law)

 Heat Flux : 𝑞

𝑥

′′

𝑑𝑑

𝑑𝑥

𝑊

𝑚

2

k : Thermal Conductivity

𝑊

𝑚∙𝑘

 Heat Rate : 𝑞

𝑥

𝑥

′′

𝑐

𝑊 A

c

: Cross-Sectional Area

Heat Convection Rate Equations (Newton's Law of Cooling)

 Heat Flux: 𝑞

′′

𝑠

𝑊

𝑚

2

h : Convection Heat Transfer Coefficient

𝑊

𝑚

2

∙𝐾

 Heat Rate: 𝑞 = ℎ𝐴

𝑠

𝑠

) 𝑊 A

s

: Surface Area 𝑚

2

Heat Radiation emitted ideally by a blackbody surface has a surface emissive power: 𝐸

𝑏

𝑠

4

𝑊

𝑚

2

 Heat Flux emitted : 𝐸 = 𝜀𝜎𝑇

𝑠

4

𝑊

𝑚

2

where ε is the emissivity with range of 0 ≤ 𝜀 ≤ 1

and 𝜎 = 5.67 × 10

𝑊

𝑚

2

𝐾

4

is the Stefan-Boltzmann constant

 Irradiation: 𝐺

𝑎𝑏𝑠

= 𝛼𝐺 but we assume small body in a large enclosure with 𝜀 = 𝛼 so that 𝐺 = 𝜀 𝜎 𝑇

𝑠𝑠𝑠

4

 Net Radiation heat flux from surface: 𝑞

𝑠𝑎𝑑

′′

𝑞

𝐴

𝑏

𝑠

𝑠

4

𝑠𝑠𝑠

4

 Net radiation heat exchange rate: 𝑞

𝑠𝑎𝑑

𝑠

𝑠

4

𝑠𝑠𝑠

4

) where for a real surface 0 ≤ 𝜀 ≤ 1

This can ALSO be expressed as: 𝑞 𝑠𝑎𝑑

𝑠

𝑠

𝑠𝑠𝑠

) depending on the application

where ℎ

𝑠

is the radiation heat transfer coefficient which is: ℎ

𝑠

𝑠

𝑠𝑠𝑠

𝑠

2

𝑠𝑠𝑠

2

𝑊

𝑚

2

∙𝐾

 TOTAL heat transfer from a surface: 𝑞 = 𝑞

𝑐𝑐𝑐𝑐

𝑠𝑎𝑑

𝑠

𝑠

𝑠

𝑠

4

𝑠𝑠𝑠

4

Conservation of Energy (Energy Balance)

𝑖𝑐

𝑔

𝑐𝑠𝑜

𝑠𝑜

(Control Volume Balance) ; 𝐸̇

𝑖𝑐

𝑐𝑠𝑜

= 0 (Control Surface Balance)

where 𝐸̇

𝑔

is the conversion of internal energy (chemical, nuclear, electrical) to thermal or mechanical energy, and

𝑠𝑜

= 0 for steady-state conditions. If not steady-state ( i.e. , transient) then 𝐸̇

𝑠𝑜

𝑝

𝑑𝑑

𝑑𝑜

Heat Equation (used to find the temperature distribution)

Heat Equation (Cartesian):

𝜕

𝜕𝑥

𝜕𝑑

𝜕𝑥

𝜕

𝜕𝜕

𝜕𝑑

𝜕𝜕

𝜕

𝜕𝜕

𝜕𝑑

𝜕𝜕

𝑝

𝜕𝑑

𝜕𝑜

If 𝑘 is constant then the above simplifies to:

𝜕

2

𝑑

𝜕𝑥

2

𝜕

2

𝑑

𝜕𝜕

2

𝜕

2

𝑑

𝜕𝜕

2

𝑞̇

𝑘

1

𝛼

𝜕𝑑

𝜕𝑜

where 𝛼 =

𝑘

𝜌𝑐

𝑝

is the thermal diffusivity

Heat Equation (Cylindrical):

1

𝑠

𝜕

𝜕𝑠

𝜕𝑑

𝜕𝑠

1

𝑠

2

𝜕

𝜕𝜕

𝜕𝑑

𝜕𝜕

𝜕

𝜕𝜕

𝜕𝑑

𝜕𝜕

𝑝

𝜕𝑑

𝜕𝑜

Heat Eqn. (Spherical):

1

𝑠

2

𝜕

𝜕𝑠

2

𝜕𝑑

𝜕𝑠

1

𝑠

2

sin 𝜃

2

𝜕

𝜕𝜕

𝜕𝑑

𝜕𝜕

1

𝑠

2

sin 𝜃

𝜕

𝜕𝜃

sin 𝜃

𝜕𝑑

𝜕𝜃

𝑝

𝜕𝑑

𝜕𝑜

Thermal Circuits

Plane Wall: 𝑅

𝑜,𝑐𝑐𝑐𝑑

𝐿

𝑘𝐴

Cylinder: 𝑅

𝑜,𝑐𝑐𝑐𝑑

ln�

𝑟

𝑟

2𝜋𝑘𝐿

Sphere: 𝑅

𝑜,𝑐𝑐𝑐𝑑

(

1

r

1

r

)

4𝜋𝑘

𝑜,𝑐𝑐𝑐𝑐

1

ℎ𝐴

𝑜,𝑠𝑎𝑑

1

𝑟

𝐴

_____________________________________________________________________________________________________________

General Lumped Capacitance Analysis

𝑠

′′

𝑠,ℎ

𝑔̇

[

4

𝑠𝑠𝑠

4

)]

𝑠(𝑐,𝑠)

Radiation Only Equation

𝜌𝜌𝑐

4 𝜀 𝐴

𝑠,𝑟

𝜎 𝑑

𝑠𝑠𝑟

3

�ln �

𝑑

𝑠𝑠𝑟

+𝑑

𝑑

𝑠𝑠𝑟

−𝑑

� − ln �

𝑑

𝑠𝑠𝑟

+𝑑

𝑖

𝑑

𝑠𝑠𝑟

−𝑑

𝑖

� + 2 �tan

𝑑

𝑑

𝑠𝑠𝑟

� − tan

𝑑

𝑖

𝑑

𝑠𝑠𝑟

Heat Flux, Energy Generation, Convection, and No Radiation Equation

𝑑−𝑑

− �

𝑏

𝑎

𝑑

𝑖

− 𝑑

− �

𝑏

𝑎

= exp(−𝑎𝑑) ; where 𝑎 = �

ℎ𝐴

𝑠,𝑐

𝜌𝜌𝑐

� and 𝑏 =

𝑞

𝑠

′′

𝐴

𝑠,ℎ

  • 𝐸̇

𝑔

𝜌𝜌𝑐

Convection Only Equation

𝑖

𝑖

= exp �− �

𝑠

𝑜

1

ℎ𝐴

𝑠

𝑜

𝑜

𝑖

� 1 − exp �−

𝑜

𝜏

𝑡

𝑚𝑎𝑥

𝑖

ℎ𝐿

𝑐

𝑘

If there is an additional resistance either in series or in parallel, then replace ℎ with 𝑈 in all the above lumped capacitance

equations, where

1

𝑅

𝑡

𝐴

𝑠

𝑊

𝑚

2

∙𝐾

� ; 𝑈 = overall heat transfer coefficient, 𝑅

𝑜

= total resistance, 𝐴

𝑠

= surface area.

Convection Heat Transfer

𝜌𝜌𝐿

𝑐

𝜇

𝜌𝐿

𝑐

𝜈

[Reynolds Number] ; 𝑁𝑁

�𝐿

𝑐

𝑘

𝑓

[Average Nusselt Number]

where 𝜌 is the density, 𝜌 is the velocity, 𝐿 𝑐

is the characteristic length, 𝜇 is the dynamic viscosity, 𝜈 is the kinematic viscosity, 𝑚̇ is the mass flow

rate, ℎ

is the average convection coefficient, and 𝑘

𝑓

is the fluid thermal conductivity.

Vertical Cylinders: the equations for the Vertical Plate can be applied to vertical cylinders of height L if the following criterion is

met:

𝜋

𝐿

35

𝐺𝑠

𝐿

1 / 4

Long Horizontal Cylinders: 𝑁𝑁

����

𝜋

= �0.60 +

  1. 387 𝑅𝑎

𝐷

1 / 6

�1+�

  1. 559

𝑃𝑟

9 / 16

8 / 27

2

; 𝑅𝑎

𝜋

≲ 10

12

[Properties evaluated at T

f

]

Spheres: 𝑁𝑁

����

𝜋

= 2 +

  1. 589 𝑅𝑎

𝐷

1 / 4

�1+�

  1. 469

𝑃𝑟

9 / 16

4 / 9

; 𝑅𝑎

𝜋

≲ 10

11

; 𝑃𝑘 ≥ 0.7 [Properties evaluated at T

f

]

Heat Exchangers

Heat Gain/Loss Equations: 𝑞 = 𝑚̇ 𝑐

𝑝

𝑐

𝑖

𝑠

𝑙𝑚

; where 𝑈 is the overall heat transfer coefficient

Log-Mean Temperature Difference: ∆𝑇

𝑙𝑚,𝑃𝑃

�𝑑

ℎ,𝑖

−𝑑

𝑐,𝑖

�−�𝑑

ℎ,𝑜

−𝑑

𝑐,𝑜

ln�

�𝑇

ℎ,𝑖

−𝑇

𝑐,𝑖

�𝑇

ℎ,𝑜

−𝑇𝑐 ,𝑜�

[Parallel-Flow Heat Exchanger]

Log-Mean Temperature Difference: ∆𝑇

𝑙𝑚,𝐶𝑃

�𝑑

ℎ,𝑖

−𝑑

𝑐,𝑜

�−�𝑑

ℎ,𝑜

−𝑑

𝑐,𝑖

ln�

�𝑇

ℎ,𝑖

−𝑇𝑐 ,𝑜�

�𝑇

ℎ,𝑜

−𝑇

𝑐,𝑖

[Counter-Flow Heat Exchanger]

For Cross-Flow and Shell-and-Tube Heat Exchangers: ∆𝑇 𝑙𝑚

𝑙𝑚,𝐶𝑃

; where 𝐹 is a correction factor

Number of Transfer Units (NTU): 𝑁𝑇𝑈 =

𝑈𝐴

𝐶

𝑚𝑖𝑚

; where 𝐶

𝑚𝑖𝑐

is the minimum heat capacity rate in [W/K]

Heat Capacity Rates: 𝐶

𝑐

𝑐

𝑝,𝑐

[Cold Fluid] ; 𝐶

𝑝,ℎ

[Hot Fluid] ; 𝐶

𝑠

𝐶

𝑚𝑖𝑚

𝐶

𝑚𝑎𝑚

[Heat Capacity Ratio]

Note: The condensation or evaporation side of the heat exchanger is associated with 𝐶

𝑚𝑎𝑥

  • If Pr ≤ 10 → n = 0.
  • If Pr ≥ 10 → n = 0.