






Study with the several resources on Docsity
Earn points by helping other students or get them with a premium plan
Prepare for your exams
Study with the several resources on Docsity
Earn points to download
Earn points by helping other students or get them with a premium plan
Community
Ask the community for help and clear up your study doubts
Discover the best universities in your country according to Docsity users
Free resources
Download our free guides on studying techniques, anxiety management strategies, and thesis advice from Docsity tutors
Complete and schematic heat transfer equation cheat sheet
Typology: Cheat Sheet
1 / 10
This page cannot be seen from the preview
Don't miss anything!
On special offer
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
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
∞
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
ℎ
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
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
ℎ
�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 +
𝐷
1 / 6
�1+�
𝑃𝑟
�
9 / 16
�
8 / 27
�
2
; 𝑅𝑎
𝜋
≲ 10
12
[Properties evaluated at T
f
Spheres: 𝑁𝑁
����
𝜋
= 2 +
𝐷
1 / 4
�1+�
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
ℎ
ℎ
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