1. Unsteady State Heat Transfer
HT3: Experimental Studies of Thermal Diffusivities and Heat Transfer Coefficients

2. Steady versus Transient Heat Transfer
Steady implies no change with time at any point within the medium
Transient implies variation with time or time dependence

3. Multidimensional Heat Transfer
Heat transfer problems are also classified as being:
one-dimensional,
two dimensional,
three-dimensional.
In the most general case, heat transfer through a medium is three-dimensional. However, some problems can be classified as two- or one-dimensional depending on the relative magnitudes of heat transfer rates in different directions and the level of accuracy desired.

4. Heat is conducted in the direction of decreasing temperature, and thus
The rate of heat conduction through a medium in a specified direction (say, in the x-direction) is expressed by Fourier’s law of heat conduction for one-dimensional heat conduction as:
Heat is conducted in the direction
of decreasing temperature, and thus
the temperature gradient is negative
when heat is conducted in the positive x-direction.
(2-1)

5. General Relation for Fourier’s Law of Heat Conduction
The heat flux vector at a point P on the surface of the figure must be perpendicular to the surface, and it must point in the direction of decreasing temperature
If n is the normal of the
isothermal surface at point P,
the rate of heat conduction at
that point can be expressed by
Fourier’s law as
(2-2)

6. General Relation for Fourier’s Law of Heat Conduction-Continue
In rectangular coordinates, the heat conduction vector can be expressed in terms of its components as
which can be determined from Fourier’s law as
(2-3)
(2-4)

7. Heat Generation Examples: Heat generation is a volumetric phenomenon.
electrical energy being converted to heat at a rate of I2R,
fuel elements of nuclear reactors,
exothermic chemical reactions.
Heat generation is a volumetric phenomenon.
The rate of heat generation units : W/m3 or Btu/h · ft3.
The rate of heat generation in a medium may vary with time as well as position within the medium.
The total rate of heat generation in a medium of volume V can be determined from
(2-5)

8. One-Dimensional Heat Conduction Equation - Plane Wall
Rate of heat
conduction
at x
Rate of heat
conduction
at x+Dx
Rate of heat
generation inside the element
Rate of change of the energy content of the element - + =
(2-6)

9. Substituting into Eq. 2–6, we get
(2-6)
The change in the energy content and the rate of heat generation can be expressed as
Substituting into Eq. 2–6, we get
(2-7)
(2-8)
(2-9)
Dividing by ADx, taking the limit as Dx 0 and Dt 0,
and from Fourier’s law:
(2-11)

10. Variable conductivity:
The area A is constant for a plane wall  the one dimensional transient heat conduction equation in a plane wall is
Variable conductivity:
(2-13)
Constant conductivity:
(2-14)
The one-dimensional conduction equation may be reduces to the following forms under special conditions
(2-15)
1) Steady-state:
2) Transient, no heat generation:
(2-16)
3) Steady-state, no heat generation:
(2-17)

11. One-Dimensional Heat Conduction Equation - Long Cylinder
Rate of heat
conduction
at r
Rate of heat
conduction
at r+Dr
Rate of heat
generation inside the element
Rate of change of the energy content of the element - + =
(2-18)

12. Substituting into Eq. 2–18, we get
(2-18)
The change in the energy content and the rate of heat generation can be expressed as
Substituting into Eq. 2–18, we get
(2-19)
(2-20)
(2-21)
Dividing by ADr, taking the limit as Dr 0 and Dt 0,
and from Fourier’s law:
(2-23)

13. Variable conductivity:
Noting that the area varies with the independent variable r according to A=2prL, the one dimensional transient heat conduction equation in a plane wall becomes
(2-25)
Variable conductivity:
Constant conductivity:
(2-26)
The one-dimensional conduction equation may be reduces to the following forms under special conditions
(2-27)
1) Steady-state:
2) Transient, no heat generation:
(2-28)
3) Steady-state, no heat generation:
(2-29)

14. One-Dimensional Heat Conduction Equation - Sphere
Variable conductivity:
(2-30)
Constant conductivity:
(2-31)

15. General Heat Conduction Equation
Rate of heat
conduction
at x, y, and z
Rate of heat
conduction
at x+Dx, y+Dy, and z+Dz
Rate of heat
generation
inside the
element
Rate of change
of the energy
content of the element - + =
(2-36)

16. Constant conductivity:
Repeating the mathematical approach used for the one-dimensional heat conduction the three-dimensional heat conduction equation is determined to be
Two-dimensional
Constant conductivity:
(2-39)
Three-dimensional
(2-40)
1) Steady-state:
2) Transient, no heat generation:
(2-41)
3) Steady-state, no heat generation:
(2-42)

17. Cylindrical Coordinates
(2-43)

18. Spherical Coordinates
(2-44)

19. Boundary and Initial Conditions
Specified Temperature Boundary Condition
Specified Heat Flux Boundary Condition
Convection Boundary Condition
Radiation Boundary Condition
Interface Boundary Conditions
Generalized Boundary Conditions

20. Specified Temperature Boundary Condition
For one-dimensional heat transfer through a plane wall of thickness L, for example, the specified temperature boundary conditions can be expressed as
T(0, t) = T1
T(L, t) = T2
(2-46)
The specified temperatures can be constant, which is the case for steady heat conduction, or may vary with time.

21. Specified Heat Flux Boundary Condition
The heat flux in the positive x-direction anywhere in the medium, including the boundaries, can be expressed by Fourier’s law of heat conduction as
Heat flux in the positive x-direction
(2-47)
The sign of the specified heat flux is determined by inspection: positive if the heat flux is in the positive direction of the coordinate axis, and negative if it is in the opposite direction.

22. Two Special Cases
Insulated boundary
Thermal symmetry
(2-49)
(2-50)

23. Convection Boundary Condition
Heat conduction
at the surface in a
selected direction
Heat convection
at the surface in the same direction =
(2-51a)
and
(2-51b)

24. Radiation Boundary Condition
Heat conduction
at the surface in a
selected direction
Radiation exchange at the surface in
the same direction =
(2-52a)
and
(2-52b)

25. Interface Boundary Conditions
At the interface the requirements are:
(1) two bodies in contact must have the same temperature at the area of contact,
(2) an interface (which is a
surface) cannot store any
energy, and thus the heat flux
on the two sides of an
interface must be the same.
TA(x0, t) = TB(x0, t)
(2-53)
and
(2-54)

26. Generalized Boundary Conditions
In general a surface may involve convection, radiation, and specified heat flux simultaneously. The boundary condition in such cases is again obtained from a surface energy balance, expressed as
Heat transfer
to the surface
in all modes
from the surface
In all modes =
Heat Generation in Solids
The quantities of major interest in a medium with heat generation are the surface temperature Ts and the maximum temperature Tmax that occurs in the medium in steady operation.

27. Heat Generation in Solids -The Surface Temperature
Rate of
heat transfer
from the solid
energy generation
within the solid =
(2-63)
For uniform heat generation within the medium
(2-64)
The heat transfer rate by convection can also be expressed from Newton’s law of cooling as -
(2-65)
(2-66)

28. Heat Generation in Solids -The Surface Temperature
For a large plane wall of thickness 2L (As=2Awall and V=2LAwall)
(2-67)
For a long solid cylinder of radius r0 (As=2pr0L and V=pr02L)
(2-68)
For a solid sphere of radius r0 (As=4pr02 and V=4/3pr03)
(2-69)

29. Heat Generation in Solids -The maximum Temperature in a Cylinder (the Centerline)
The heat generated within an inner cylinder must be equal to the heat conducted through its outer surface.
(2-70)
Substituting these expressions into the above equation and separating the variables, we get
Integrating from r =0 where T(0) =T0 to r=ro
(2-71)

30. Heat Equation
The Heat Equation
A differential equation whose solution provides the temperature distribution in a stationary medium.
Based on applying conservation of energy to a differential control volume
through which energy transfer is exclusively by conduction.
Cartesian Coordinates:
(2.13)
Thermal energy
generation
Change in thermal
energy storage
Net transfer of thermal energy into the
control volume (inflow-outflow)

31. Generalized Heat Diffusion Equation
If we perform a heat balance on a small volume of material…
… we get:
heat conduction in T
heat conduction
out
heat generation
rate of change
of temperature
heat cond.
in/out
heat
generation
thermal diffusivity

32. Heat Equation (Radial Systems)
Cylindrical Coordinates:
(2.20)
Spherical Coordinates:
(2.33)

33. Heat Equation (Special Case)
One-Dimensional Conduction in a Planar Medium with Constant Properties
and No Generation

34. Boundary and Initial Conditions
Boundary Conditions
Boundary and Initial Conditions
For transient conduction, heat equation is first order in time, requiring
specification of an initial temperature distribution:
Since heat equation is second order in space, two boundary conditions
must be specified. Some common cases:
Constant Surface Temperature:
Constant Heat Flux:
Applied Flux
Insulated Surface
Convection

35. Boundary Conditions Tbody
Heat transfer boundary conditions generally come in three types:
q = 20 W/m2
specified heat flux
Neumann condition
q = h(Tamb-Tbody)
external heat transfer
coefficient
Robin condition
T = 300K
specified temperature
Dirichlet condition
Tbody

36. Transient Heat Conduction
Many heat conduction problems encountered in engineering applications
involve time as in independent variable. The goal of analysis is to determine the variation of the temperature as a function of time and position T (x, t) within the heat conducting body. In general, we deal with conducting bodies in a three dimensional Euclidean space in a suitable set of coordinates (x ∈ R3) and the goal is to predict the evolution of the temperature field for future times (t > 0).
Here we investigate solutions to selected special cases of the following form of the heat equation
Solutions to the above equation must be obtained that also satisfy suitable initial and boundary conditions.

37. Example: Point Thermal Explosion
Let a fixed amount of energy H0(J) be instantaneously released (thermal explosion) at time t = 0
at the origin of a three dimensional system of coordinates inside a solid body of infinite extent initially at T (X, 0) = T (r, 0) = 0 everywhere, where, 𝐗=r= 𝑥 2 + 𝑦 2 + 𝑧 2 . No other thermal energy input exists subsequent to the initial instantaneous release. Assuming constant thermal properties k (thermal conductivity), r (density) and Cp (heat capacity), the heat equation is:
where a = k/rCp is thermal diffusivity [m2/s].
This must be solved subject to the initial condition T (r, 0) = 0 for all r > 0 plus the statement
expressing the instantaneous release of energy at t = 0 at the origin. Since the body is infinitely large, the far field temperature never changes and all the released energy must dissipate within the body itself. The fundamental solution of this problem is given by:
𝜏= 𝑟 2 𝛼 - characteristic time
where H0/rCp is the amount of energy released per unit energy required to raise the temperature of a unit volume of material by one degree.
This solution may be useful in the study of thermal explosions where a buried explosive load located at r = 0 is suddenly released at t = 0 and the subsequent distribution of temperature at various distances from the explosion is measured as a function of time. A slight modification of the solution leads to the problem of surface heating of bulk samples by short duration pulses of finely focused high energy beams.

38. One-Dimensional Problems
Imposed Boundary Temperature in Cartesian Coordinates: A simple but important conduction heat
transfer problem consists of determining the temperature history inside a solid flat wall which is quenched from a high temperature. More specifically, consider the homogeneous problem of finding the one-dimensional temperature distribution inside a slab of thickness L and thermal diffusivity a, initially at some specified temperature T (x, 0) = f(x) and exposed to heat extraction at its boundaries x = 0 and x = L such that T (0, t) = T (L, t) = 0 (Dirichlet homogeneous conditions), for t > 0. The thermal properties are assumed constant.
Convection at the Boundary in Cartesian Coordinates: Same geometry BUT the boundary conditions
specify values of the normal derivative of the temperature or when linear combinations of the normal derivative and the temperature itself are used. Consider the homogeneous problem of transient heat conduction in a slab initially at a temperature T = f(x) and subject to convection losses into a medium at T = 0 at x = 0 and x = L. Convection heat transfer coefficients at x = 0 and x = L are, respectively h1 and h2. Assume the thermal conductivity of the slab k is constant.
Imposed Boundary Temperature and Convection at the Boundary in Cylindrical Coordinates:
a long cylinder (radius r = b) initially at T = f(r) whose surface temperature is made equal to zero for t > 0.
A long cylinder (radius r = b) initially at T = f(r) is exposed to a cooling medium which extracts heat uniformly from its surface.
Imposed Boundary Temperature and Convection at the Boundary in Spherical Coordinates:
quenching problem where a sphere (radius r = b) initially at T = f(r) whose surface temperature is made equal to zero for t > 0.
Consider a sphere with initial temperature T (r, 0) = f(r) and dissipating heat by convection into a medium at its surface r = b.

39. Characteristic Length

40. First Problem: Slab/Convection
The first problem is the 1D transient homogeneous heat conduction in a plate of span L from
an initial temperature Ti and with one boundary insulated and the other subjected to a convective heat flux condition into a surrounding environment at T∞. This problem is equivalent to the quenching of a slab of span 2L with identical heat convection at the external boundaries x = −L and x = L).
The mathematical formulation of the problem is to find T (x, t) such that:
Boundary conditions:
−𝑘 𝜕𝑇 𝜕𝑥 + h(T- 𝑇 ∞ )=0
Initial conditions:
for all x when t = 0,
Introduction of the following non dimensional parameters simplifies the mathematical formulation of the problem. The dimensionless distance (X), time (t) and temperature (q):
and a Biot number:
The Biot number (Bi) is a dimensionless number used in heat transfer calculations.
It is named after the French physicist Jean-Baptiste Biot (1774–1862), and gives a simple index
of the ratio of the heat transfer resistances inside (1/k) of and at the surface of a body (1/hL).
Biot number smaller than 0.1 imply that the heat conduction inside the body is much faster than
the heat convection away from its surface, and temperature gradients are negligible inside of it.

41. First Problem Formulation: Slab/Convection
Boundary conditions:
−𝑘 𝜕𝑇 𝜕𝑥 + h(T- 𝑇 ∞ )=0
Initial conditions:
for all x when t = 0,
Introduction of the following non dimensional parameters simplifies the mathematical formulation of the problem. The dimensionless distance (X), time (t) and temperature (q) and a Biot number:
With the new variables, the mathematical formulation of the heat conduction problem becomes:
and

42. Second Problem Formulation: Solid Cylinder/Convection
1D transient homogeneous heat conduction in a solid cylinder of radius b from an
initial temperature Ti and with one boundary insulated and the other subjected to a
convective heat flux condition into a surrounding environment at T∞.
Boundary conditions:
−𝑘 𝜕𝑇 𝜕𝑥 + h(T- 𝑇 ∞ )=0
Introduction of the following non dimensional parameters simplifies the mathematical formulation of the problem. The dimensionless distance (X), time (t) and temperature (q) and a Biot number:
With the new variables, the mathematical formulation of the heat conduction problem becomes:

43. Third Problem Formulation: Sphere/Convection
Cooling of a sphere (0 ≤ r ≤ b) initially at a uniform temperature Ti and subjected to a uniform
convective heat flux at its surface into a medium at T∞ with heat transfer coefficient h.
In terms of the new variable U(r, t) = rT (r, t) the mathematical formulation of the problem is:
Introduction of the following non dimensional parameters simplifies the mathematical formulation of the problem. The dimensionless distance (X), time (t) and temperature (q) and a Biot number:
With the new variables, the mathematical formulation of the heat conduction problem becomes:

44. Biot number

45. Fo = Diffusive transport rate (a/L2)/storage rate (1/t)
Fourier number
In physics and engineering, the Fourier number (Fo) or Fourier modulus, named after Joseph Fourier, is a dimensionless number that characterizes heat conduction. Conceptually, it is the ratio of diffusive/conductive transport rate by the quantity storage rate and arises from non-dimensionalization of the heat equation. The general Fourier number is defined as:
Fo = Diffusive transport rate (a/L2)/storage rate (1/t)
The thermal Fourier number is defined by the conduction rate to the rate of thermal energy storage:
Compare with non-dimensionless time parameter:
So Fo=t
𝜕 2 𝜃 𝜕 𝑋 2 = 𝜕𝜃 𝜕𝐹𝑜
To understand the physical significance of the Fourier number t, we may express it as
Therefore, again the Fourier number is a measure of heat conducted through a body relative to heat stored. Thus, a large value of the Fourier number indicates faster propagation of heat through a body.

46. Lumped System Analysis
if the internal temperature of a body remains relatively constant with respect to distance
– can be treated as a lumped system analysis
– heat transfer is a function of time only, T = T (t)
Typical criteria for lumped system analysis is Bi< 0.1
In heat transfer analysis, some bodies are observed to behave like a “lump” whose interior temperature remains essentially uniform at all times during a heat transfer process. The temperature of such bodies can be taken to be a function of time only, T(t). Heat transfer analysis that utilizes this idealization is known as lumped system analysis , which provides great simplification in certain classes of heat transfer problems without much sacrifice from accuracy.
Consider a small hot copper ball coming out of an oven. Mea-
surements indicate that the temperature of the copper ball changes with time, but it does not change much with position at any given time. Thus the temperature of the ball remains nearly uniform at all times, and we can talk about the temperature of the ball with no reference to a specific location.

47. Lumped System Analysis
If Bi< 0.1
Consider a body of arbitrary shape of mass m, volume V, surface area As, density r, and specific heat cp initially at a uniform temperature Ti . At time t = 0, the body is placed into a medium at temperature T∞, and heat transfer takes place between the body and its environment, with a heat transfer coefficient h. For the sake of discussion, we assume that T >Ti, but the analysis is equally valid for the opposite case. We assume lumped system analysis to be applicable, so that the temperature remains uniform within the body at all times and changes with time only, T= T(t). During a differential time interval dt, the temperature of the body rises by a differential amount dT. An energy balance of the solid for the time interval dt can be expressed as:
𝑙𝑛 𝑇 𝑡 − 𝑇 ∞ 𝑇 𝑖 − 𝑇 ∞ =-Bi∙Fo or or
Integrating from t=0, at which T =Ti, to any time t, at which T=T(t), gives
The reciprocal of b has
time unit, and is called
the time constant. or
The temperature of a body approaches the ambient temperature T
exponentially. The temperature of the body changes rapidly at the
beginning, but rather slowly later on. A large value of b indicates that the
body approaches the environment temperature in a short time. The larger
the value of the exponent b, the higher the rate of decay in temperature.
Note that b is proportional to the surface area, but inversely proportional
to the mass and the specific heat of the body. This is not surprising since
it takes longer to heat or cool a larger mass, especially when it has a
large specific heat.

48. Lumped System Analysis
If Bi< 0.1
(A)
Once the temperature T(t) at time t is available, the rate of convection heat transfer between the body and its environment at that time can be
determined from Newton’s law of cooling as:
(B)
The total amount of heat transfer between the body and the surrounding medium over the time interval t 0 to t is simply the change in the energy content of the body:
The amount of heat transfer reaches its upper limit when the body reaches the surrounding temperature T. Therefore, the maximum heat transfer between the body and its surroundings is
We could also obtain this equation by substituting the T(t) relation from Eq. A into the 𝑄
relation in Eq. B and integrating it from t =0 to t → ∞.

49. Exact Solution of One-Dimensional Transient Conduction Problem
The non-dimensionalized partial differential equation formulated above together with its boundary and
initial conditions can be solved using several analytical and numerical techniques, including the Laplace or other transform methods, the method of separation of variables, the finite difference method, and the finite-element method.
Here we discuss the method of separation of variables developed by J. Fourier in 1820s and is based on
expanding an arbitrary function (including a constant) in terms of Fourier series. The method is applied
by assuming the dependent variable to be a product of a number of functions, each being a function of a single independent variable. This reduces the partial differential equation to a system of ordinary differential equations, each being a function of a single independent variable.
In the case of transient conduction in a plain wall, for example, the dependent variable is the solution
function u(X, t), which is expressed as u(X, t)= F(X)G(t), and the application of the method results in two ordinary differential equation, one in X and the other in t.
The method is applicable if (1) the geometry is simple and finite (such as a rectangular block, a cylinder, or a
sphere) so that the boundary surfaces can be described by simple mathematical functions, and (2) the differential equation and the boundary and initial conditions in their most simplified form are linear (no terms that involve products of the dependent variable or its derivatives) and involve only one nonhomogeneous term (a term without the dependent variable or its derivatives).

50. Separation of Variables
Let us consider the Slab/Convection experiment. Recall that in this case we have:
The heat conduction equation in cylindrical or spherical coordinates can be nondimensionalized in a similar way. Note that nondimensionalization reduces the number of independent variables and parameters from 8 to 3—from x, L, t, k, a, h, Ti, and T to X, Bi, and Fo. That is,
This makes it very practical to conduct parametric studies and to present results in graphical form. Recall that in the case of lumped system analysis, we had u f(Bi, Fo) with no space variable.

51. Separation of Variables
First, we express the dimensionless temperature function u(X, t) as a product of a function of X only and a function of t only as:
Substituting to:
all the terms that depend on X are on the left-hand side of the equation and all the terms that depend on t are on the r the terms that are function of different variables are separated (and thus the name separation of variables). Considering that both X and t can be varied independently, the equality in Eq. C can hold for any value of X and t only if it is equal to a constant. Further, it must be a negative constant that we will indicate by -l2 since a positive constant will cause the function G(t) to increase indefinitely with time (to be infinite), which is unphysical, and a value of zero for the constant means no time dependence, which is again inconsistent with the physical problem. Setting Eq. C equal to -l2 gives:
whose general solutions are:
and
(C)
we have

52. Separation of Variables
Then it follows that there are an infinite number of solutions of the form , and the solution of this linear heat conduction problem is a linear combination of them,
The constants An are determined from the initial condition
This is a Fourier series expansion that expresses a constant in terms of an infinite series of cosine functions. Now we multiply both sides of last eq. by cos(lmX), and integrate from X=0 to X=1. The right-hand side involves an infinite number of integrals of the form:
It can be shown that all of these integrals vanish except when n m, and the coefficient An becomes:

53. Separation of Variables
This completes the analysis for the solution of one-dimensional transient heat conduction problem in a plane wall. Solutions in other geometries such as a long cylinder and a sphere can be determined using the same approach. The results for all three geometries are summarized in Table.
Note that the solution for the plane wall is also applicable for a plane wall of thickness L whose left surface at x =0 is insulated and the right surface at x=L is subjected to convection since this is precisely the mathematical problem we solved.

54. Approximate Analytical Solutions
The analytical solutions of transient conduction problems typically involve infinite series, and thus the evaluation of an infinite number of terms to determine the temperature at a specified location and time. However, as demonstrated in Table, the terms in the summation decline rapidly as n and thus ln increases because of the exponential decay function . This is especially the case when the dimensionless time t is large. Therefore, the evaluation of the first few terms of the infinite series (in this case just the first term) is usually adequate to determine the dimensionless temperature q. For example, for t> 0.2, keeping the first term and neglecting all the remaining terms in the series results in an error under 2 percent.
We are usually interested in the solution for times with t> 0.2, and thus it is very convenient to express the solution using this one-term approximation, given as:
where the constants A1 and l1 are functions of the Bi number only, and their values are listed in Table (see next slide) against the Bi number for all three geometries. The function J0 is the zeroth-order Bessel function of the first kind (see next slide).

55. Useful Tables

56. Approximate Analytical Solutions
Noting that cos (0)= J0(0)= 1 and the limit of (sin x)/x is also 1, these relations simplify to the next ones at the center of a plane wall, cylinder, or sphere:
Comparing the sets of equations above with approximate solution we notice that the dimensionless temperatures anywhere in a plane wall, cylinder, and sphere are related to the center temperature by
which shows that time dependence of dimensionless temperature within a given geometry is the same throughout. That is, if the dimensionless center temperature q0 drops by 20 percent at a specified time, so does the dimensionless temperature q0 anywhere else in the medium at the same time. Once the Bi number is known, these relations can be used to determine the
temperature anywhere in the medium.

57. Graphical Solutions : Heisler Charts
The solutions obtained for 1D non homogeneous problems with Neumann boundary conditions in Cartesian coordinate systems using the method of separation of variables have been collected and assembled in the form of transient temperature nomographs by Heisler. The given charts are a very useful baseline against, which to validate one’s own analytical or numerical computations.
Indeed, the determination of the constants A1 and l1 usually requires interpolation. For those who prefer reading charts to interpolating, these relations are plotted and the one-term approximation solutions are presented in graphical form, known as the transient temperature charts.
The transient temperature charts shown in next slides for a large plane wall, long cylinder, and sphere were presented by M. P. Heisler in 1947 and are called Heisler charts.
There are three charts associated with each geometry: the first chart is to determine the temperature T0 at the center of the geometry at a given time t. The second chart is to determine the temperature at other locations at the same time in terms of T0. The third chart is to determine
the total amount of heat transfer up to the time t. These plots are valid for t > 0.2.

58. with a convection coefficient of h.
Transient temperature and heat transfer charts for a plane wall of thickness 2L initially at a uniform
temperature Ti subjected to convection from all sides to an environment at temperature T∞
with a convection coefficient of h.

59. with a convection coefficient of h.
Transient temperature and heat transfer charts for a long cylinder of radius ro initially at a uniform
temperature Ti subjected to convection from all sides to an environment at temperature T∞
with a convection coefficient of h.

60. with a convection coefficient of h.
Transient temperature and heat transfer charts for a sphere of radius ro initially at a uniform
temperature Ti subjected to convection from all sides to an environment at temperature T∞
with a convection coefficient of h.

61. Useful Relationship
Again the temperature of the body changes from the initial temperature Ti to the temperature of the surroundings T∞ at the end of the transient heat conduction process and the maximum amount of heat that a body can gain (or lose) is simply the change in the energy content of the body:
The amount of heat transfer Q at a finite time t is
Assuming constant properties, the ratio of Q/Qmax becomes
Using the appropriate non-dimensional temperature relations based on the one term
approximation for the plane wall, cylinder, and sphere, and performing the indicated integrations, we obtain the following relations for the fraction of heat transfer in those geometries:
These Q/Qmax ratio relations based on the one-term approximation are also plotted in Heisler charts, against the variables Bi and h2at/k2 for the large plane wall, long cylinder, and sphere, respectively. Note that once the fraction of heat transfer Q/Qmax has been determined from these charts or equations for the given t, the actual amount of heat transfer by that time can be evaluated by multiplying this fraction by Qmax.