314: Thermodynamics of Materials

Classical and statistical thermodynamics; entropy and energy functions in liquid and solid solutions, and their applications to phase equilibria. Lectures, problem solving. Materials science and engineering degree candidates may not take this course for credit with or after CHEM 342 1. (new stuff)

Course Outcomes

1 314: Thermodynamics of Materials

At the conclusion of the course students will be able to:

articulate the fundamental laws of thermodynamics and use them in basic problem solving.
discriminate between classical and statistical approaches.
describe the thermal behavior of solid materials, including phase transitions.
use thermodynamics to describe order-disorder transformations in materials .
apply solution thermodynamics for describing liquid and solid solution behavior.

2 Introduction

The content and notation of these notes is based on the excellent book, “Thermodynamics in Materials Science”, by Robert DeHoff [3]. The notes provided here are a complement to this text, and are provided so that the core curriculum of the undergradaute Materials Science and Engineering program can be found in one place (http://msecore.northwestern.edu/). These notes are designed to be self-contained, but are more compact than a full text book. Readers are referred to DeHoff's book for a more complete treatment.

3 Big Ideas of Thermodynamics

The following statements sum up some of foundational ideas of thermodynamics:

Energy is conserved
Entropy is produced
Temperature has an absolute reference at 0 - at which all substances have the same entropy

3.1 Classification of Systems

Systems can be classified by various different properties such as constituent phases and chemical components, as described below.

Chemical components
- Unary system has one chemical component
- Multicomponent system has more than one chemical component

image: 4_home_ken_Mydocs_MSEcore_314_figures_syscomp.svg

Figure 3.1: Unary system (left) and multicomponent system (right).

Phases

Homogeneous system has one phase

Heterogeneous system has more than one phase

image: 5_home_ken_Mydocs_MSEcore_314_figures_sysphase.svg

Figure 3.2: Homogeneous system (left) and heterogeneous system (right).

Energy and mass transfer: closed and open systems:

image: 6_home_ken_Mydocs_MSEcore_314_figures_open_closed_isolated.svg

Figure 3.3: Open, closed and isolated thermodynamic systems.

Reactivity
- Non-reacting system contains components that do not chemically react with each other
- Reacting system contains components that chemically react with each other

image: 7_home_ken_Mydocs_MSEcore_314_figures_sysreact.svg

Figure 3.4: Non-reacting system (left) and reacting system (right).

Another classification is between simple and complex systems. For instance, complex systems may involve surfaces or fields that lead to energy exchange.

3.2 Thermodynamic State Variables

Thermodynamic state variables are properties of a system that depend only on current condition, not history. Temperature,

T

, is an obvious example, since we know intuitively that the temperature in a room has the same meaning to us, now matter what the previous temperature history actually was. Other state variables include the pressure,

P

, and the system volume,

V

. For example, two states

A

and

A^{'}

, each with their own characteristic values of

P,

V

and

T

\begin{matrix} \begin{matrix} A & \to & A^{'} \\ P, V, T & P^{'}, V^{'}, T^{'} \end{matrix} & (3.1) \end{matrix}

The values of the pressure difference

Δ P = P^{'} - P

= is independent of the path that the system takes to move from state

A

A^{'}

. The same is true for

Δ V

and

Δ T

. Note that because state variables are often functions of other variables, they are often referred to as state functions of these other variables. For our purposes the terms 'state function' and 'state variable' can be used interchangeably.

3.3 Process Variables

Work and heat are examples of process variables.

Work (

W

) - Done on the system. Note that our sign convention here is that work done ON the system is positive.

Heat (

Q)

- Absorbed or emitted. The sign convention in this case is that heat absorbed by the system is positive.

Their values for a process depend on the path.

3.3.1 Work Done by an External Force

The work done by an external force is the force multiplied by distance over which the force acts. In other words, the force only does work if the body it is pushing against actually moves in the direction of the applied force. In differential form we have:

\begin{matrix} δ W = \vec{F} \cdot d \vec{x} & (3.2) \end{matrix}

Note that

\vec{F}

and

\vec{x}

are vector quantities, but

W

is a scalar quantity. As a reminder, the dot product appearing in Eq. 3.2 is defined as follows:

\begin{matrix} \vec{A} \cdot \vec{B} = | \vec{A} | | \vec{B} | cos θ & (3.3) \end{matrix}

where

θ

is the angle between the two vectors, illustrated in Figure 3.5.

image: 8_home_ken_Mydocs_MSEcore_314_figures_Dot_Product.svg

Figure 3.5: Definition of the angle

θ

between two vectors.

The total work is obtained by integrating

δ W

over the path of the applied force:

\begin{matrix} W = \underset{p a t h}{\int_{⏟}} \vec{F} \cdot d \vec{x} & (3.4) \end{matrix}

For example, when we lift a from the floor to the table as illustrated in Figure 3.6 we increase the gravitational potential energy,

U

, of the barbell by an amount

m g h

, where:

$m$ = the mass of the barbell
$g$ = the gravitational acceleration (9.8 m/s $^{2}$ )
$h_{f}$ = the final resting height of the barbell above the floor

Because the potential energy only depends only on the final resting location of the barbell, it is a state variable. The work we expend in putting the barbell there depends on the path we took to get it there, however. As a result this work is NOT a state function. Suppose, for example that we lift the barbell to a maximum height

h_{m a x}

and then drop it onto the table. The work,

W

, we expended is equal to

m g h_{m a x}

, which is greater than the increase in potential energy,

Δ U

. The difference between between

W

and

Δ U

is the irreversible work and corresponds to energy dissipated as heat, permanent deformation of the table, etc. We'll return to the distinction between reversible and irreversible work later.

image: 9_home_ken_Mydocs_MSEcore_314_figures_barbell.svg

Figure 3.6: Work done on a barbell.

3.3.2 Work Done by an Applied Pressure

Another important example of work is the work done by an external force in changing the volume of the system that is under a state of hydrostatic pressure. The easiest and most important example to describe is a gas that is being compressed by a piston as shown in Figure 3.7. Equation 3.2 still applies in this case, but the force in this case is given by the product of the area and pressure:

\begin{matrix} \vec{F} = P \vec{A} & (3.5) \end{matrix}

It may seem strange to write the area as a vector, but it is just reminding us that the pressure acts perpendicular to the surface, so the direction of

\vec{A}

is perpendicular to the surface of the piston. Combining Eq. 3.5 with Eq. 3.2 gives:

\begin{matrix} δ W = P \vec{A} \cdot d \vec{x} & (3.6) \end{matrix}

The decrease in volume of the gas is given by

\vec{A} \cdot d \vec{x}

, so we can replace

\vec{A} \cdot d \vec{x}

with

- d V

to obtain:

\begin{matrix} δ W = - P d V & (3.7) \end{matrix}

This result is an important one that we will use quite a bit later on.

image: 10_home_ken_Mydocs_MSEcore_314_figures_piston.svg

Figure 3.7: Work done by force on a piston.

3.4 Extensive and Intensive Properties

Extensive properties depend on size or extent of the system. Examples include the volume (

V)

, mass (

m)

internal energy (

U

) and the entropy (

S

). Intensive properties are defined at a point, with examples including the temperature (

T

) and the pressure

(P

) and the mass density,

ρ

Extensive properties can be defined as integrals of intensive properties. For example the mass is obtained by integration of the mass density over the total volume:

\begin{matrix} m = \int_{V}^{V} ρ (\vec{r}) ⅆ \vec{r} & (3.8) \end{matrix}

Also, intensive properties can be obtained from combinations of extensive properties. For example

C_{k}

, the molar concentration of component

k

, is the ratio of two extensive quantities:

n_{k}

the total number of moles of component

k

and the volume:

\begin{matrix} C_{k} \equiv lim_{V \to 0} \frac{n_{k}}{V} & (3.9) \end{matrix}

This approach works for the density as well, with the mass density,

ρ

, given by the ratio of the sample mass,

m

, to the sample volume,

V

\begin{matrix} ρ \equiv lim_{V \to 0} \frac{m}{V} & (3.10) \end{matrix}

4 The Laws of Thermodynamics

Outcomes for this section:

State the first, second and third laws of thermodynamics.
Write a combined statement of the first and second laws in differential form.
Given sufficient information about how a process is carried out, describe whether entropy is produced or transferred, whether or not work is done on or by the system, and whether heat is absorbed or released.
Quantitatively relate differentials involving heat transfer/production, entropy transfer/production, and work.

4.1 First Law of Thermodynamics

The first law of thermodynamics is that energy is conserved. This means that the increase in the internal energy of the system is equal to the sum of the heat flow, the work done on the system and the heat flow into the system. In mathematical terms:

\begin{matrix} Δ U = Q + W + W^{'} & (4.1) \end{matrix}

image: 11_home_ken_Mydocs_MSEcore_314_figures_1stlaw.svg

Figure 4.1: Conservation of energy

where:

$Δ U$ = Internal energy change of the system

$Q =$ Heat flow into the system

$W =$ Mechanical work done by surroundings on the system ( $P_{e x t})$

W^{'} =

All other reversible work done on the system

4.2 Second Law of Thermodynamics

The second law of thermodynamics states

that entropy can be transferred or produced, but not destroyed, so the total entropy change in the universe (

Δ S_{u n i}

) cannot be negative:

\begin{matrix} Δ S_{u n i} \geq 0 & (4.2) \end{matrix}

Here

Δ S_{u n i}

includes the system of interest and its surroundings, as illustrated in Figure 4.2.

\begin{matrix} Δ S_{u n i} = [Δ S_{t}^{'} + Δ S_{p}^{'}] + [Δ S_{t} + Δ S_{p}] & (4.3) \end{matrix}

We write the entropy this way to differentiate between entropy produced in the system and surroundings (

Δ S_{p}

and

Δ S_{p}^{'}

) and entropy that is transfered between the system and surroundings (

Δ S_{t}

and

Δ S_{t}^{'}

$Δ S_{p}$ : entropy produced in the system
$Δ S_{p}^{'}$ : entropy produced in the surroundings
$Δ S_{t}$ : entropy transferred to the system
$Δ S_{t}^{'}$ : entropy transferred to the surroundings

image: 12_home_ken_Mydocs_MSEcore_314_figures_2ndlaw.svg

Figure 4.2: Transfer of entropy

The entropy change for a process can only be zero (for a reversible process) or positive (for an irreversible process) in the universe at large, which includes the systems and the surroundings. In mathematical terms:

\begin{matrix} Δ S_{u n i} = Δ S_{p}^{'} + Δ S_{p} \geq 0 & (4.4) \end{matrix}

For infinitesimal changes (very small

Δ

), we replace

Δ

with the differential,

d

. We do this because we can always obtain the total change in a quantity,

Δ

, by integrating over the differential. For example, to calculate the entropy difference between state

A

and state

B

we have:

\begin{matrix} Δ S_{s y s} [A \to B] = \int_{A}^{B} ⅆ S_{s y s} & (4.5) \end{matrix}

That that while the overall entropy change (system + surroundings) cannot be negative, the system entropy change can be negative, if is compensated for by an appropriate increase in the entropy of the surroundings. In differential terms,

d S_{s y s} = d S_{t} + d S_{p}

where

d S_{s y s}

can be negative.

4.2.1 Reversible and Irreversible Processes

Irreversible processes produce entropy, whereas reversible processes (an idealization) do not. Entropy necessarily increases over time. The rate of entropy production is one measure of how far we are from equilibrium.

Processes carried out very slowly, and which remain very close to equilibrium approach the ideal of reversibility. A perfectly reversible process is extremely useful for calculations, and has the following characteristics.

No entropy is produced
No permanent changes take place in the universe

To compute differences in state functions, for example the specific path between state

A

and state

B

in Eq. 4.5 one can chose the simplest path between the two states, which is the reversible path.

4.2.2 Entropy and Heat

The second law of thermodynamics is defined in terms of entropy, but we haven't yet defined what entropy really is. The statistical approach described in Section 9 will shed some light on entropy, but for now we will just introduce the following simple but remarkably important relationship between a differential change in the heat content and the differential change in the entropy:

\begin{matrix} d S = \frac{δ Q}{T} & (4.6) \end{matrix}

This equation a mathematical statement of the second law of thermodynamics. Qualitatively, it is easy to see that Eq. 4.6 is consistent with what know from common experience. For example, we know that a metal bar that is hot at one end and cold at the other end is not at equilibrium, since over time heat will flow from the hot end to the cold end. Consider a simplistic model of this where heat is flowing between one region at a temperature of

T_{1}

, and a second region at a temperature

T_{2}

, with

T_{2} > T_{1}

. When a certain heat increment

δ Q

moves from region 1 to 2, the entropy in region 1 decreases by

δ Q / T_{1}

, while the entropy in region 2 increases by

δ Q / T_{2}

. The net change in entropy is given:

\begin{matrix} δ S = δ Q / T_{2} - δ Q / T_{1} & (4.7) \end{matrix}

This is positive whenever

T_{1} > T_{2}

, which is consistent with our starting point where the heat was moving from region 1 to region 2. So when heat moves from a hot region to a cold region, the entropy increases, as we know it must for a non-equilibrium process.

4.3 Third Law of Thermodynamics

The third law of thermodynamics states that there is an absolute lower limit to the temperature of matter, and the entropy of all substances is the same at that temperature. In more practical terms,

S = 0

T

=0K (absolute zero) for all materials.

The fact that we can use absolute zero as a reference temperature for the entropy is quite useful in a variety of situations. It can be used, for example, to provide information about the nature of a chemical reaction. Consider, for example,the following simple chemical reaction, where silicon reacts with carbon to form silicon carbide:

S i + C \to S i C

Consider the following 4-step process, which begins and ends with Si and C as separate elements at T=0K (see Fig. :

I: Heating Si and C from 0K to the reaction temperature, $T_{1}$ .
II: Reaction of Si and C to form SiC at $T = T_{1}$
III: Cooling the SiC from $T_{1}$ to 0K.
IV: A (hypothetical) splitting of the SiC back into Si and C at 0K.

Because we start and end at the same place, and because entropy is a state function, the overall entropy for the cyclic process consisting of all 4 steps is equal to zero:

\begin{matrix} Δ S_{c y c} = Δ S_{I} + Δ S_{I I} + Δ S_{I I I} + Δ S_{I V} = 0 & (4.8) \end{matrix}

We also know that

Δ S_{I V} = 0,

since the reaction takes place at =0K, where all materials have

S = 0

. As a result we have:

\begin{matrix} Δ S_{I I} = - Δ S_{I} - Δ S_{I I I} & (4.9) \end{matrix}

image: 13_home_ken_Mydocs_MSEcore_314_figures_3rdlaw.svg

Figure 4.3: Cyclic process involving formation of silicon carbide.

The quantity

Δ S_{I}

is the difference between the entropy of the starting compounds (Si and C) at

T_{1}

, compared to the value of the entropy of these compounds at 0K, so

Δ S_{I}

is simply

S_{S i}

S_{C}

. Similarly,

Δ S_{I I I} = - S_{S i C}

, with the negative sign arising from the fact that process III corresponds to a reduction in the temperature from

T_{1}

to 0K. Finally,

Δ S_{I I}

is, the entropy change associated the SiC-forming reaction, so we have:

\begin{matrix} Δ S_{S i + C \to S i C} (T_{1}) = S_{S i C} (T_{1}) - S_{S i} (T_{1}) - S_{C} (T_{1}) & (4.10) \end{matrix}

Δ S

for the reaction is simply the difference between the entropy of the products and reactants at the appropriate temperature. Entropies of different compounds are measurable quantities, as are other thermodynamic function state functions discussed later in the text.

4.4 Differential Quantities

In differential form the first law of thermodynamics (Eq. 4.1) is as follows:

\begin{matrix} d U = δ Q + δ W + δ W^{'} & (4.11) \end{matrix}

We can combine this with the expression from the second law from

δ Q

\begin{matrix} δ Q = T d S & (4.12) \end{matrix}

We also have the following expression for the work done by an external pressure,

P

, on changing the volume,

V :

\begin{matrix} δ W = - P d V & (4.13) \end{matrix}

Combination of Eqs. 4.11-4.13 can be combined to give the following combined statement of the first and second laws:

\begin{matrix} d U = T d S - P d V + δ W^{'} & (4.14) \end{matrix}

From this equation we see that at constant system entropy (

d S = 0

) and volume (

d V = 0

) the change in internal energy is equal to the non-mechanical reversible work done on the system. In general, entropy and volume are not constant, which is why we more commonly use other thermodynamic potentials as described in the following section.

Finally, if we will assume that there is no additional work done on the system apart from work done by the external pressure (

δ W^{'} = 0)

, we have:

\begin{matrix} d U = T d S - P d V & (4.15) \end{matrix}

5 Thermodynamic Variables and Relations

Outcomes for this section:

Derive differentials of state functions ( $V$ , $S$ , $U$ , $F$ , $H$ , $G$ ) in terms of $d P$ and $d T$ .
Using the Maxwell relations, relate coefficients in the differentials of state functions.
Define the coefficient of thermal expansion, compressibility, and heat capacity of a material.
Express the differential of any given state function in terms of the differentials of two others.
Define reversible, adiabatic, isotropic, isobaric, and isothermal processes.
Calculate changes in state functions by defining reversible paths (if necessary) and integrating differentials for (a) an ideal gas, and (b) materials with specified $α$ , $β$ , and $C_{P} (T)$ . (Multiple examples are given for ideal gas, solids, and liquids.)
Special emphasis (Example 4.13): calculate the change in Gibbs free energy when one mole of a substance is heated from room temperature to an arbitrary temperature at constant pressure.
Describe the origin of latent heat, and employ this concept in the calculation of changes in Gibbs free energy $G$ .

5.1 Enthalpy

The enthalpy,

H

, is defined in the following way:

\begin{matrix} H \equiv U + P V & (5.1) \end{matrix}

The total differential of the enthalpy is:

\begin{matrix} d H = d U + P d V + V d P & (5.2) \end{matrix}

Now we eliminate

d U

by using Eq. 4.14:

\begin{matrix} d H = T d S + V d P + δ W^{'} & (5.3) \end{matrix}

For a process at constant

P,

d P = 0

(constant pressure, or isobaric ), and if no other work is done

δ W^{'} = 0

. Under these conditions we have:

\begin{matrix} d H_{p} = T d S_{p} = δ Q_{p} & (5.4) \end{matrix}

where the '

p

' subscripts indicate that the differential quantities are being evaluated at constant pressure. The enthalpy therefore measures the reversible heat exchange in an isobaric process.

5.2 Helmholtz Free Energy

The Helmholtz free energy is defined in the following way:

\begin{matrix} F \equiv U - T S & (5.5) \end{matrix}

In differential form this becomes:

\begin{matrix} d F = d U - T d S - S d T & (5.6) \end{matrix}

\begin{matrix} d F = - S d T - P d V + δ W^{'} & (5.7) \end{matrix}

For a process carried out at constant T (isothermal ),

d T = 0

\begin{matrix} d F_{T} = - P d V_{T} + δ W_{T}^{'} = δ W_{T} + δ W_{T}^{'} = δ W_{T, t o t} & (5.8) \end{matrix}

F_{T}

reports the total (reversible) work done on the system.

5.3 Gibbs Free Energy

The Gibbs free energy,

G

, is defined in the following way.

\begin{matrix} G \equiv U + P V - T S = H - T S & (5.9) \end{matrix}

\begin{matrix} d G = d U + V d P + P d V - T d S - S d T & (5.10) \end{matrix}

\begin{matrix} = (T d S - P d V + δ W^{'}) + V d P + P d V - T d S - S d T & (5.11) \end{matrix}

\begin{matrix} d G = - S d T + V d P + δ W^{'} & (5.12) \end{matrix}

For processes carried out under isothermal and isobaric (constant

P

) conditions

(d T, d P = 0)

, then

\begin{matrix} d G_{T, P} = δ W_{T, P}^{'} & (5.13) \end{matrix}

G

reports the total work done other than mechanical work, e.g. chemical reactions and phase transformations.

5.4 Other Material Properties

5.4.1 Volume thermal expansion coefficient

Here we define some material properties that relate different thermodynamic state variables to one one another. The first is the thermal expansion coefficient,

α

, which describes the temperature dependence of the volume:

\begin{matrix} α \equiv \frac{1}{V} {(\frac{\partial V}{\partial T})}_{P} (K^{- 1}) & (5.14) \end{matrix}

5.4.2 Isothermal Compressibility

The isothermal compressibility,

β

, gives the relationship between the pressure and the volume :

\begin{matrix} β \equiv \frac{1}{V} {(\frac{\partial V}{\partial P})}_{T} (P a^{- 1}) & (5.15) \end{matrix}

5.4.3 Heat Capacity

The heat capacity is the amount of energy needed to change temperature by some amount. Two different heat capacities are typically defined. The first of these,

C_{P}

, corresponds to a process performed at a constant pressure:

\begin{matrix} δ Q_{P} \equiv C_{P} d T_{P} & (5.16) \end{matrix}

Here

T_{P}

indicates that the pressure is being held constant. If the process is reversible, then

d Q_{P} = T d S

(Eq. 4.12), and we have:

\begin{matrix} T d S = C_{P} d T_{p} & (5.17) \end{matrix}

Because the process is happening at constant pressure, we can rewrite Eq. 5.17 in the following way:

\begin{matrix} \frac{C_{P}}{T} = {(\frac{\partial S}{\partial T})}_{P} & (5.18) \end{matrix}

Empirically,

C_{P}

is described by four parameters,

a, b,

c and

d

. These four parameters are a convenient way of tabulating the data.

\begin{matrix} C_{P} (T) = a + b T + \frac{c}{T^{2}} + d T^{2} & (5.19) \end{matrix}

The constant volume heat capacity,

C_{V}

, is defined in a similar way, but with the volume held constant instead of the temperature:

\begin{matrix} δ Q_{V} \equiv C_{V} d T_{V} & (5.20) \end{matrix}

The corresponding version of Eq. 5.18 is:

\begin{matrix} \frac{C_{V}}{T} = {(\frac{\partial S}{\partial T})}_{V} & (5.21) \end{matrix}

Note that

C_{P}

is necessarily larger than

C_{V}

. At constant

P

, the volume increases with increasing temperature, so work is done on the surroundings. Therefore, more energy is needed to achieve the same

Δ T

. The relationship between

C_{P}

and

C_{V}

is obtained below in section 5.6.3.

5.5 Coefficient Relations

A variety of relationships exist between the different thermodynamic functions. These relationships are a consequence of some basic mathematical relationships. Suppose that we have a function,

Z

of two variables

X

and

Y

\begin{matrix} Z = Z (X, Y) & (5.22) \end{matrix}

The differential of

Z

s given by:

\begin{matrix} d Z = {. \frac{\partial Z}{\partial X} |}_{Y} d X + {. \frac{\partial Z}{\partial Y} |}_{X} d Y & (5.23) \end{matrix}

The differential forms of

U

(Eq. 4.15) ,

F

(Eq. )

H

(Eq. ) and

G

(Eq. ) all have the form of Eq. 5.23. The various relationships between the thermodynamic potentials (

U

F

G,

H)

can be summarized by the thermodynamic square shown in Figure 5.1. Our description of how to use it is taken directly from the appropriate Wikipedia page (https://en.wikipedia.org/wiki/Thermodynamic_square)[2].

image: 14_home_ken_Mydocs_MSEcore_314_figures_maxwellrelations.svg

Figure 5.1: Thermodynamic square used to help determine thermodynamic relations.

Start in the portion of the square corresponding the thermodynamic potential of interest. In our case we'll use

U

The two opposite corners of the potential of interest represent the coefficients of the overall result. In our case these are

P

and

T

. When the coefficient lies on the left hand side of the square, we use the negative sign that is shown in the diagram. In our example we have

d U = - P [d i f f e r e n t i a l] + T [d i f f e r e n t i a l]

. Now we just have to figure out what the two differentials are.

The differentials are obtained by moving to the opposite corner of the corresponding coefficient. In our case we have $V$ opposite $P$ and $S$ opposite $T$ , so we end up with $d U = - P d V + T d S$ , which is what we expect to get from Eq. 4.14. We can then use this same procedure to obtain the expressions given previously for $d H$ , $d F$ and $d G$ . Note that two variables on the opposite sides of the thermodynamic square are thermodynamically conjugate variables [1], with have units of energy when multiplied by one another.

We can also use the thermodynamic square of Fig. 5.1 to obtain a variety of expressions for the partial derivatives of the different thermodynamic potentials. The procedure is as follows:

Identify the potential you are interested in, just as before. We'll again take $U$ as our example.
We can differentiate with respect to either of the variables adjacent to the potential we chose. For $U$ we can differentiate with respect to $S$ or $V$ , with the other one of these two variables remaining constant during the differentiation.
The result of the differentiation is given by the variable that is conjugate to (diagonally across from) the variable we are differentiating by. For example, if we differentiate $U$ by $S$ we have , we have ${. (\partial U / \partial S) |}_{V} = T$ . The following 8 expressions are obtained in this way:

\begin{matrix} \begin{matrix} T = {(\frac{\partial U}{\partial S})}_{V}, & - P = {(\frac{\partial U}{\partial V})}_{S} \\ T = {(\frac{\partial H}{\partial S})}_{P}, & V = {(\frac{\partial H}{\partial P})}_{S} \\ - S = {(\frac{\partial F}{\partial T})}_{V}, & - P = {(\frac{\partial F}{\partial V})}_{T} \\ - S = {(\frac{d G}{\partial T})}_{P}, & V = {(\frac{\partial G}{\partial P})}_{T} \end{matrix} & (5.24) \end{matrix}

The thermodynamic square can be used to illustrate one more set of relationships, referred to as the Maxwell relationships . Consider a state variable

Z

, which is a function of two other variables,

X

and

Y .

A property of state functions is that the order of differentiation doesn't matter, so we have:

\begin{matrix} \frac{\partial^{2} Z}{\partial X \partial Y} = \frac{\partial^{2} Z}{\partial Y \partial X} & (5.25) \end{matrix}

We can rewrite this as:

\begin{matrix} \frac{\partial}{\partial X} {(\frac{\partial Z}{\partial Y})}_{X} = \frac{\partial}{\partial Y} {(\frac{\partial Z}{\partial X})}_{Y} & (5.26) \end{matrix}

Suppose the functions

M

and

N

are defined in the following way:

\begin{matrix} M = {(\frac{\partial Z}{\partial X})}_{Y}, N = {(\frac{\partial Z}{\partial Y})}_{X} & (5.27) \end{matrix}

By comparing Eqs. 5.26 and 5.27 we obtain the following expression.

\begin{matrix} {(\frac{\partial M}{\partial Y})}_{X} = {(\frac{\partial N}{\partial X})}_{Y} & (5.28) \end{matrix}

The expressions for the differentials of the internal energy (

U

), Enthalpy (

H

), Helmoltz free energy (

F

), and Gibbs free energy

(G

) all have the form of Eq. 5.23, with values of

M

and

N

given in Eq. 5.24. Use of Eq. 5.28 in each of these four cases gives the following relationships between the appropriate partial derivatives:

5.5.1 Internal Energy

\begin{matrix} d U = T d S - P d V \to {(\frac{\partial T}{\partial V})}_{S} = - {(\frac{\partial P}{\partial S})}_{V} & (5.29) \end{matrix}

5.5.2 Enthalpy

\begin{matrix} d H = T d S + V d P \to {(\frac{\partial T}{\partial P})}_{S} = {(\frac{\partial V}{\partial S})}_{P} & (5.30) \end{matrix}

5.5.3 Helmholtz Free Energy

\begin{matrix} d F = - S d T - P d V \to {(\frac{\partial S}{\partial V})}_{T} = {(\frac{\partial P}{\partial T})}_{V} & (5.31) \end{matrix}

5.5.4 Gibbs Free Energy

\begin{matrix} d G = - S d T + V d P \to - {(\frac{\partial S}{\partial P})}_{T} = {(\frac{\partial V}{\partial T})}_{P} & (5.32) \end{matrix}

5.6 Equation of State Relationships

The ideal gas law is an example of an equation of state , where one thermodynamic variable (a dependent variable ) is expressed in terms of two other thermodynamic variables (the independent variables ). Equations of state can also be expressed in differential form, where differential changes in dependent variable are expressed in terms of differentials of the dependent variables. In general, once we know the equation of state for one combination of one independent and two dependent variables, we can express any thermodynamic function in terms of any two thermodynamic variables.

5.6.1 Expression for $d S$

It will be useful in many of our following derivations to have a general expression for

d S

in terms of

d P

and

d T

. We begin by expressing

d S

in terms of the appropriate partial derivatives:

\begin{matrix} d S = {(\frac{\partial S}{\partial T})}_{P} d T + {(\frac{\partial S}{\partial P})}_{T} d P & (5.33) \end{matrix}

We can use Eq. 5.32 to replace

{(\frac{\partial S}{\partial P})}_{T}

with

- {(\frac{\partial V}{\partial T})}_{P}

\begin{matrix} d S = {(\frac{\partial S}{\partial T})}_{P} d T - {(\frac{\partial V}{\partial T})}_{P} d P & (5.34) \end{matrix}

Now we can use the definition of the thermal expansion coefficient,

α

, (Eq. 5.14) to replace

{(\frac{\partial V}{\partial T})}_{P}

with

V α

\begin{matrix} d S = {(\frac{\partial S}{\partial T})}_{P} d T - V α d P & (5.35) \end{matrix}

Finally, we use the definition of the constant pressure heat capacity,

C_{p}

, (Eq. 5.18) to replace

{(\frac{\partial S}{\partial T})}_{P}

with

\frac{C_{P}}{T}

, which yields the following relationship expressiong

d S

in terms of

d T

and

d P

, and which involves the two material properties,

α

and

C_{P}

\begin{matrix} d S = \frac{C_{P}}{T} d T - V α d P & (5.36) \end{matrix}

5.6.2 Expression for $d V$

The differential of the volume in terms of

d T

and

d P

can also be obtained in a similar manner to the approach described above for obtaining

d S

. We start with the following expression for

d V

\begin{matrix} d V = {(\frac{\partial V}{\partial T})}_{P} d T + {(\frac{\partial V}{\partial P})}_{T} d P & (5.37) \end{matrix}

The two partial derivatives in this expression appear in the definitions of the volume thermal expansion coefficient,

α

, and the isothermal compressibility,

β

. With

α = \frac{1}{V} {(\frac{\partial V}{\partial T})}_{P}

and

β = - \frac{1}{V} {(\frac{\partial V}{\partial P})}_{T}

we can rewrite Eq. 5.37 in the following way:

\begin{matrix} d V = α V d T - β V d P & (5.38) \end{matrix}

5.6.3 Relationship between $C_{P}$ and $C_{V}$

In order to determine the relationship between the constant pressure heat capacity,

C_{P}

and its constant volume counterpart,

C_{V}

, we need to get an expression for the

d S

with temperature and volume as the dependent variables instead of temperature and pressure. We do this by using Eq. 5.38 to get an expression for

d P

\begin{matrix} d P = \frac{α}{β} d T - \frac{d V}{β V} & (5.39) \end{matrix}

This expression for

d P

can be substituted into Eq. 5.36 for

d S

to give:

\begin{matrix} d S = (\frac{C_{P}}{T} - \frac{V α^{2}}{β}) d T + \frac{α}{β} d V & (5.40) \end{matrix}

From this we see that

{(\frac{\partial S}{\partial T})}_{V} = \frac{C_{P}}{T} - \frac{V α^{2}}{β} .

We get the constant-volume heat capacity,

C_{V}

, from it's definition in Eq. 5.21:

\begin{matrix} C_{V} = T {(\frac{\partial S}{\partial T})}_{V} = C_{P} - \frac{T V α^{2}}{β} & (5.41) \end{matrix}

Note that

C_{V} < C_{P}

, as mentioned earlier.

6 The Ideal Gas

We begin to apply these principles by considering an ideal gas , which obeys the following constitutive relationship:

\begin{matrix} P V = n R T & (6.1) \end{matrix}

Here

n

is the number of moles and

R

is the gas constant :

\begin{matrix} \begin{matrix} R = 8.314 (J / m o l \cdot K) \\ = 1.987 (c a l / m o l \cdot K) \\ = 0.08206 (l - a t m / m o l \cdot K) \end{matrix} & (6.2) \end{matrix}

If n=1, then

P V = R T

, where

V = V_{m}

, where

V_{m}

is the molar volume.

6.1 Thermal Expansion Coefficient of an Ideal Gas

We get the volume thermal expansion coefficient ,

α

, by substituting the ideal gas constitutive law into Eq. 5.14:

\begin{matrix} α = \frac{1}{V} {(\frac{\partial V}{\partial T})}_{P} = \frac{P}{n R T} \frac{\partial}{\partial T} {(\frac{n R T}{P})}_{P} = \frac{P}{n R T} \cdot \frac{n R}{P} = \frac{1}{T}, & (6.3) \end{matrix}

We see that the volume thermal expansion coefficient of an ideal gas is simply equal to the inverse of the absolute temperature.

6.2 Compressibility of an Ideal Gas

A very simple expression is also obtained for the isothermal compressibility of an ideal gas, in this case substituting the ideal gas constitutive equation into Eq. 5.15:

\begin{matrix} β = - \frac{1}{V} {(\frac{\partial V}{\partial P})}_{T} = - \frac{P}{n R T} \frac{\partial}{\partial P} {(\frac{n R T}{P})}_{T} = - \frac{P}{n R T} (\frac{- n R T}{P^{2}}) = \frac{1}{P} & (6.4) \end{matrix}

The isothermal also has a very simple form for an ideal gas, equal to the inverse of the pressure.

6.3 Internal Energy of Ideal Gas

To calculate the internal energy for an ideal gas, the first step is to rewrite the expression for

d U

with

T

and

P

as the dependent variables. We begin with the following expression the first and second laws (Ex. 4.15):

\begin{matrix} d U = T d S - P d V & (6.5) \end{matrix}

Using Eq. 5.36 for

d S

and Eq. 5.38 for

d V

gives:

\begin{matrix} d U = (C_{p} - P V α) d T + V (P β - T α) d P & (6.6) \end{matrix}

This expression is general for any constitutive law. For an ideal gas, we also have

α = 1 / T

and

β = 1 / P

(see previous sections), which gives:

\begin{matrix} d U = (C_{p} - \frac{P V}{T}) d T & (6.7) \end{matrix}

We also have

P V = n R T

for the ideal gas, so we have:

\begin{matrix} d U = (C_{p} - n R) d T & (6.8) \end{matrix}

We see from this result that the internal energy of an ideal gas is independent of the pressure. From Eq.5.41 we see that

C_{V} = C_{P} - \frac{T V α^{2}}{β}

, which for an ideal gas gives:

\begin{matrix} C_{V} = C_{P} - \frac{P V}{T} = C_{p} - n R & (6.9) \end{matrix}

∴ d U = C_{V} d T,

and

C_{V} = \frac{3}{2} R

One can then integrate to find that

Δ U= \frac{3}{2} R (T_{2} - T_{1})

C_{V}

is constant

For an ideal gas, the internal energy depends only on the temperature.

6.4 Specific Heat of Ideal Gas

\begin{matrix} C_{V} = C_{P} - \frac{T {(V α)}^{2}}{β} = C_{P} - R & (6.10) \end{matrix}

We will show that

C_{v} = \frac{3}{2} R

for a monatomic ideal gas. Therefore,

C_{P} = \frac{3}{2} R + R = \frac{5}{2} R

Example:

Calculate the change in T when 1 mole of gas is compressed reversible and adiabatically (no heat flow) from

V_{1}

V_{2} .

Solution:

In Example 4.6, we found that

d S = \frac{C_{V}}{T} d T + \frac{α}{β} d V

, which simplifies to

d T_{S} = - \frac{T α}{C_{V} β} d V_{S}

for a reversible, iso-entropic process, for which

d S = 0)

. For an ideal gas,

α = \frac{1}{T}

β = \frac{1}{P}

, so

d T_{S} = \frac{- T}{C_{V}} \frac{P}{T} d V_{S} = - \frac{P}{C_{V}} d V_{S .}

But

P = \frac{R T}{V}

\Rightarrow d T_{S} = \frac{- R T}{C_{V}} \frac{d V_{S}}{V}

. Evaluate by integrating.

\int_{T_{1}}^{T_{2}} \frac{d T_{S}}{T} = \frac{- R}{C_{V}} \int_{V_{1}}^{V_{2}} \frac{d V_{S}}{V} \to ln (\frac{T_{2}}{T_{1}}) = \frac{- R}{C_{V}} ln (\frac{V_{2}}{V_{1}})

ln (\frac{T_{2}}{T_{1}}) = ln [{(\frac{V_{2}}{V_{1}})}^{- R / C_{V}}] \Rightarrow \frac{T_{2}}{T_{1}} = {(\frac{V_{1}}{V_{2}})}^{\frac{R}{C_{V}}}

C_{V} = \frac{3}{2} R

T_{2} = T_{1} {(\frac{V_{1}}{V_{2}})}^{R / C_{V}} = T_{1} {(\frac{V_{1}}{V_{2}})}^{2 / 3}

(\frac{V_{1}}{V_{2}}) > 1

for compression , so T increases.

If the gas expands (

V_{2} > V_{1})

, then T decreases. One can also derive T(P) and P(V).

6.5 Some Examples of Ideal Gas Behavior

6.5.1 Free expansion of an ideal gas

[vh] Add text to discuss boundary conditions and why they are important (before listing the boundary conditions for the example). Why each physical condition corresponds to the corresponding boundary condition.

image: 15_home_ken_Mydocs_MSEcore_314_figures_ex4_9.svg

Figure 6.1: Free expansion of an ideal gas - the valve is opened at

t_{2}

and fills both chambers

Walls are rigid:

δ W = 0

Walls are insulating:

δ Q = 0

System is closed.

\Rightarrow Δ S_{t} = 0

Δ U = 0

\Rightarrow

Δ T = 0

(ideal gas)

The gas expands irreversibly.

Entropy is produced, but

Δ S

is not process dependent because

S

is a state function.

What is

Δ S

when 1 mole of gas expands freely to twice its volume? (recall

Δ T = 0) .

d S = \frac{C_{V}}{T} d T + \frac{α}{β} d V

d T = 0

P V = R T

\frac{P}{T} = \frac{R}{V}

d S = \frac{α}{β} d V_{T} = \frac{P}{T} d V_{T} = \frac{R}{V} d V_{T}

Δ S_{T} = \int_{V_{1}}^{V_{2}} \frac{R}{V} ⅆ V = R ln (\frac{V_{2}}{V_{1}}) = R ln (\frac{2 V_{1}}{V_{1}}) = R ln 2

∴ Δ S_{T} = 5.76

J/mol-K

This change for a reversible isothermal process is the same as for an irreversible free expansion in an isolated system. S is a state function.

6.5.2 Isothermal Compression of an Ideal Gas

How much heat is absorbed/released when 1 mole of gas is compressed isothermally from 1 to 25 bar at 300K?

To find heat, use S:

δ Q_{r e v, T} = T d S_{T}

d S = \frac{C_{P}}{T} d T - V^{α} d P = - V^{α} d P_{T}

The volume change is unknown, so use

V = \frac{R T}{P}

d S_{T} = \frac{- R T}{P} \frac{1}{T} d P = - R \frac{d P}{P}

Δ S_{T} = - R \int_{P_{i}}^{P_{f}} \frac{d P}{P} = - R ln (\frac{P_{f}}{P_{i}})

\to Δ Q_{r e v, T} = - R T ln (\frac{P_{f}}{P_{i}}) = - (8.314 J / m o l - K) 298 K ln (\frac{25}{1}) = - 7.975 kJ/mol

6.5.3 Reversibility requires work/heat

The piston in Figure 6.2 below may be withdrawn very slowly to maintain equilibrium.

image: 16_home_ken_Mydocs_MSEcore_314_figures_heat.svg

Figure 6.2: Piston-cylinder device

Δ U = 0 \to Δ T = 0

Δ S = \int_{V_{i}}^{V_{f}} \frac{n R}{V} ⅆ V = n R ln (\frac{V_{f}}{V_{i}})

But no entropy can be produced, so heat flow is needed to maintain T (for free expansion, T decreases)

So actually,

Δ U = Q + W = 0

\to W = - Q < 0

The system does negative work! Heat flow is positive (inward).

image: 17_home_ken_Mydocs_MSEcore_314_figures_irrvsrev.svg

Figure 6.3: Irreversible Process (top) and reversible process (bottom)

Irreversible process	Reversible process
$Δ Q = 0$	$Δ Q \neq 0$
W=0	$W \neq 0$
$Δ U = 0$	$Δ U = 0$
$Δ T = 0$	$Δ T = 0$

Table 1: Irreversible vs reversible process characteristics

Δ U = 0 \to W = - Δ Q

W < 0, Δ Q > 0

\to Δ S_{t} > 0

What is the amount of heat required to raise the temperature to 1000K isobarically?

δ Q_{r e v, P} = T d S_{p} \equiv C_{P} d T_{P}

C_{P} = \frac{5}{2} R

Δ Q_{r e v, P} = C_{P} Δ T = \frac{5}{2} R Δ T = \frac{5}{2} (8.314 J / m o l - K) \times (1000 - 298) K

Note that

d H = C_{P} d T + V (1 - T_{α}) d P

. For

d P = 0

d H = C_{P} d T

\to

Enthalpy measures reversible heat flow in absence of work. This will be useful in the analysis of solids heated under conditions of constant pressure.

6.5.4 Some useful relations for heat flow

δ Q_{r e v, T} = T d S_{T} = d U_{T} - d F_{T}

δ Q_{r e v, T} = T d S_{P} \equiv C_{P} d T_{P} = d H_{P}

(δ W^{'} = 0)

δ Q_{r e v, V} = T d S_{V} \equiv C_{V} d T_{V} = d U_{V}

(δ W^{'} = 0)

Example 4.3: Relate S(P,V)

d S = M d P + N d V

d S = M d P + N (V^{α} d T - V β d P) = (M - N V_{β}) d P + N V^{α} d T

d S = - V^{α} d P + \frac{C_{P}}{T} d T

\to

N = \frac{C_{P}}{V^{α} T} = {(\frac{\partial S}{\partial V})}_{P}

M - N V β = - V^{α}

M = - V^{α} + \frac{C_{P}}{V_{α} T} V β

M = \frac{C_{P} β}{α T} - V^{α} = {(\frac{\partial S}{\partial P})}_{V}

d S = (\frac{C_{P} β}{α T} - V^{α}) d P + \frac{C_{P}}{V^{α} T} d V

Luijten examples

$Q$ for $Δ P$ at constant $T$

Reversible, $\to δ Q_{r e v, T} = T d S$

Use $S (T, P)$ like 4.10(a)
Find $Δ T$ given $Δ P$ at constant S

Use $S (T, V)$ , also idela gas law (~4.8)
Free expansion of ideal gas, find $Δ S$ for $Δ V$

$S (T, V)$ (4.9)
Adiabatic reversible compression of a solid.

$T (S, P)$ $d S = 0,$ $Δ P$ given (4.14)
Change in G for heating at constant $P$

$G (P, T),$ $d P = 0$ (4.13)

$d G = - S d T + V d P$ , need to find $S (T)$

P V = R T

Problem: 1 mole of gas expands at an initial temperature of 300 K, from 1 l to 2 l at constant

S

. What is the final temperature?

Solution:

d S = M d T + N d P = 0

(\frac{C_{P}}{T} - \frac{{(V^{α})}^{2}}{P}) d T + \frac{α}{β} d V = 0

α = \frac{1}{T}

β = \frac{1}{P}

\frac{C_{V}}{T} d T = - \frac{α}{β_{C_{V}}} d V

\frac{d T}{T} = \frac{- α}{β_{C_{V}}} d V

\frac{d T}{T} = \frac{- P}{T_{C_{V}}} d U

d T = - \frac{P}{C_{V}} d V

Use

P V = R T

to get to two variables

P = \frac{R T}{V}

C_{V} = \frac{3}{2} R

d T = \frac{- R T}{C_{V} V} d V =

\frac{d T}{T} = \frac{- R}{3 / 2 R} \frac{d V}{V} = \frac{- 2}{3} \frac{d V}{V}

\int_{T_{1}}^{T_{2}} \frac{d T}{T} = - \frac{2}{3} \int_{V_{1}}^{V_{2}} \frac{d V}{V}

\to ln (\frac{T_{2}}{T_{1}}) = ln {(\frac{V_{1}}{V_{2}})}^{2 / 3}

\frac{V_{1}}{V_{2}} = \frac{1}{2}

T_{2} = T_{1} {(\frac{1}{2})}^{2 / 3} = 189

Note

P_{1} = \frac{300 \cdot R}{1 0^{- 3} m^{3}} = 3 \times 1 0^{5} R

P_{2} = \frac{189 R}{2 \times 1 0^{- 3} m^{3}} = 0.95 \times 1 0^{5} R

Pressure drops by threefold

↓ P V ↑ = R T ↓

1 mole Fe is compressed reversibly. What is the change in T?

P_{1} = 1

atm,

P_{2} = 1 0^{5}

atm

d S = \frac{C_{p}}{T} d T - V^{α} d P

\frac{d T}{T} = \frac{V^{α}}{C_{P}} d P

need exponential values

Does

C_{P}

vary with

T

\frac{d C_{P}}{d T} \approx 0

, then

ln (\frac{T_{2}}{T_{1}}) = \frac{V^{α}}{C_{P}} Δ P

α = 36 \times 1 0^{- 6} K^{- 1}

C_{P} \approx 45.3 J / m o l - K

Otherwise,

\int \frac{C_{P}}{T} ⅆ T = V^{α} Δ P

V = \frac{3.1 c m^{3}}{m o l} = 7.1 \times 1 0^{- 6} m^{3} / m o l e

T_{2} = T_{1} \times 1.006 = 300 K

7 Solids and Liquids

Let's begin with an example of the calculation of the free energy as a function of temperature for a substance

Compute

Δ G

when 1 mole of MgO is heated from 300K to temperature T at constant pressure.

Solution:

d G = - S d T + V d P

d P = 0

d G_{P} = - S d T_{P} = - S (T) d T_{P}

But

C_{P}

depends on temperature

\to

so does S.

d S = \frac{C_{P}}{T} d T - V^{α} d P = \frac{C_{P}}{T} d T

{(\frac{\partial S}{\partial T})}_{P} = \frac{C_{P}}{T}

S = S_{o} + \int \frac{C_{P} (T)}{T} ⅆ T

C_{P} = a + b T, S_{o} = 26.8 J / m o l - K

S = S_{o} + \int_{T_{1}}^{T_{2}} ⅆ T (\frac{a}{T} + b)

Evaluate expression, substitute data at the end

S = S_{o} + \int \frac{C_{P} (T)}{T} ⅆ T = S_{o} + \int_{T_{1}}^{T_{2}} ⅆ T (\frac{a}{T} + b)

S = S_{o} + a ln (\frac{T_{2}}{T_{1}}) + b (T_{2} - T_{1})

T_{1} = 300 K, T_{2} = T

S (T) = S (300 K) + a ln (\frac{T}{300}) + b (T - 300)

\equiv a ln T + b T + \underset{constant}{\underset{⏟}{[S_{o} - a ln 300 - 300 b]}}

C_{P} (T)_{M g O} = \underset{a}{\underset{⏟}{48.99}} + \underset{b}{\underset{⏟}{3.43 \times 1 0^{- 3} T}} - \underset{ignored}{\underset{⏟}{\frac{11.34 \times 1 0^{- 5}}{T^{2}}}} (\frac{J}{m o l - K})

Δ G = \int_{300}^{T} ⅆ G = - \int_{300}^{T_{f}} S (T) ⅆ T = - \int_{300}^{T_{f}} (a ln T + b T + C) ⅆ T

= [a (T ln T - T) + \frac{1}{2} b T^{2} + c T]_{T_{f}}^{300}

Δ G = a T ln T + \frac{1}{2} b T^{2} + (C - a) T = - 300 a ln 300 - \frac{1}{2} b (300)^{2} - (C - a) 300

↑

Check this, see also sec 7.3 p. 180

a = 48.99 \frac{J}{m o l - K}, b = 3.43 \times 1 0^{- 3} \frac{J}{m o l K^{2}}

C = 26.8 J / m o l - K - a ln 300 - 300 b

Consider the following exothermic reaction (referred to as the Thermite reaction ), where Aluminum reacts with iron oxide to form aluminum oxide and iron.

2 A l + F e_{2} O_{3} \to A l_{2} O_{3} + 2 F e

How hot will this system get as the reaction proceeds? We'll do this in two parts. First, we'll calculate the heat generated in the reaction, then we'll figure out how much this heat will increase the temperature of the system.

Consider the change in enthalpy for each half-reaction:

\underline{\begin{matrix} 2 A l + \frac{3}{2} O_{2} \to A l_{2} O_{3} & Δ H_{1} = - 1675.7 \frac{k J}{m o l} \\ F e_{2} O_{3} \to 2 F e + \frac{3}{2} O_{2} & Δ H_{2} = 823 \frac{k J}{m o l} \end{matrix}}

2 A l + \frac{3}{2} O_{2} + F e_{2} O_{3} \to A l_{2} O_{3} + 2 F e + \frac{3}{2} O_{2}

Δ H = (- 1675.1 + 823) \frac{k J}{m o l} = - 852.3 \frac{k J}{m o l}

The minus sign implies that the reaction is exothermic. Now that we know how much heat is generated, we can figure out what the state of the system will be. Note that Fe melts at

1809

K and boils at 3343 K, and

A l_{2} O_{3}

melts at 2325 K. We need to determine to what temperature the system will rise assuming that all heat generated by the reaction is absorbed by the system.

Step 1: Heat

F e

and

A l_{2} O_{3}

to the melting point of

F e .

Δ H_{A l_{2} O_{3}, 1} = \int_{289}^{1809} C_{P} (T) ⅆ T = 183, 649 J

Δ H_{F e, 1}

involves 3 sub-steps: (2 moles)

↑ α \to γ

2 \int_{289}^{1187} C_{P, α} ⅆ T + Δ H_{α \to γ}

↑ γ \to δ

2 \int_{1187}^{1164} C_{P, γ} ⅆ T + Δ H_{γ \to δ}

↑ δ \to l

2 \int_{1664}^{1809} C_{P, δ} ⅆ T + Δ H_{m e l t}

C_{P, δ} = C_{P}, α

Considering the three integrals of T and three latent heats,

Δ H_{F e, 1} = 157, 741

J (for 2 moles)

So through step 1, we have

Δ H_{F e, 1} + Δ H_{A l_{2} O_{3}, 1} = 341.390

Step 2: Heat

F e

and

A l_{2} O_{3}

to melting point of

A l_{2} O_{3} .

Δ H_{A l_{2} O_{3}, 2} = \int_{1809}^{2325} C_{P, A l} ⅆ T + Δ H_{A l_{2} O_{3}} (S \to l) = (71, 240 + 107, 000) J

Δ H_{F e, 2} = 2 \int_{1809}^{2325} C_{P, F e (l)} ⅆ T = 43, 178 J

How much is left?

852, 300 - 341, 390 - 221, 418 = 289, 492

Step 3: How much energy is needed to get to the boiling point of Fe?

272, 600 J {\begin{matrix} Δ H_{F e, 3} = 2 \int_{2325}^{3343} C_{P, F e} (l) ⅆ T \\ Δ H_{A l_{2} O_{3}, 3} = \int_{2325}^{3343} C_{P, A l_{2} O_{3}} (l) ⅆ T \end{matrix}

leaving 16.892 J

How much Fe evaporates?

\frac{Q}{Δ H_{F e} (l \to g)} = \frac{16, 892 J}{340, 159 J} = 0.05

moles or 5%

Δ H (T) = Δ a T + \frac{Δ b}{2} T^{2} - Δ C \frac{1}{T} + \frac{Δ d}{3} T^{3} - Δ D

Δ D = Δ H (T_{o}) - [Δ a T_{o} + \frac{Δ b}{2} T_{o}^{2} - Δ C \frac{1}{T_{o}} + \frac{Δ d}{3} T_{o}^{3}]

2 A l + F e_{2} O_{3} \to 2 F e + A l_{2} O_{3}

Exothermic

Compute the final state and temperature assuming adiabataic, reversible reaction at constant pressure.

d T, Q = 0, d P = 0

Need initial

S, C_{P}

image: 18_home_ken_Mydocs_MSEcore_314_figures_tempflow.svg

Figure 7.1: Thermite reaction

Exothermic implies

Δ T

from heat released.

d S = M d T + N d P

d H = T d S + V d P + δ W^{'}

2 A l + \frac{3}{2} O_{2} \to A l_{2} O_{3}

Δ H_{1} = - 1875

kJ/mol

2 F e + \frac{3}{2} O_{2} \to F e_{2} O_{3}

Δ H_{2} = - 823.4

kJ/mol

2 A l + F e_{2} O_{3} \to 2 F e + A l_{2} O_{3}

2 A l + \frac{3}{2} O_{2} \to A l_{2} O_{3}

;

Δ H_{1}

\underline{F e_{2} O_{3} \to 2 F e + \frac{3}{2}} O_{2}

;

- Δ H_{2}

2 A l + F e_{2} O_{3} + \frac{3}{2} O_{2} \to A l_{2} O_{3} + 2 F e + \frac{3}{2} O_{2}

Δ H_{1} - Δ H_{2} = - 852.3 k J / m o l

δ Q_{r e v, P} = - T d S = d H

Heat is reversibly absorbed by the system.

Δ H_{F e, 1} = \int ⅆ H = \int_{298}^{1809} C_{P} ⅆ T = 157, 741

J for 2 mol

Include

Δ H

due to increasing T as well as due to phase transitions. For

A l_{2} O_{3}

, just

\int C_{P} ⅆ T

Δ H_{A l_{2} O_{3}} = 183, 649

For a total change of 341,390 J

Now heat

A l_{2} O_{3}

to melting point, and heat

F e (l)

\int C_{P} ⅆ T + Δ H_{m e l t}

Step 2 takes: 221,418 J

852,300 J is provided by the reaction:

852, 300 - 221, 418 - 341, 390 = 289, 492

image: 19_home_ken_Mydocs_MSEcore_314_figures_FeandAl2O3.svg

Figure 7.2: Changes in enthalpy in Fe and

A l_{2} O_{3}

d S = \frac{C_{V}}{T} d T + \frac{α}{β} d V = \frac{3}{2} \frac{R}{T} d T + \frac{P}{T} d V = \frac{3}{2} \frac{R}{T} d T + \frac{R}{V} d V

Good for constant V: relate

Δ S

to T change.

For constant T: relate

Δ S

to volume change.

For constant S, dS=0

{(\frac{T_{2}}{T_{1}})}^{3 / 2} = (\frac{V_{1}}{V_{2}})

\frac{T_{2}}{T_{1}} = {(\frac{V_{1}}{V_{2}})}^{2 / 3}

\frac{T_{2}}{T_{` 1}} = \frac{V_{2}}{V_{1}} \frac{P_{2}}{P_{1}}

{(\frac{P_{2}}{P_{1}})}^{3 / 2} {(\frac{V_{2}}{V_{1}})}^{3 / 2} = \frac{V_{1}}{V_{2}} \to {(\frac{P_{2}}{P_{1}})}^{3 / 2} = {(\frac{V_{1}}{V_{2}})}^{5 / 2}

\frac{P_{2}}{P_{1}} = {(\frac{V_{1}}{V_{2}})}^{5 / 3}

T_{1} V_{1}^{γ - 1} = T_{2} V_{2}^{γ - 1}

T_{1}^{\frac{γ}{1 - γ}} P_{1} = T_{2}^{\frac{γ}{1 - γ}} P_{2}

P_{1} V_{1}^{γ} = P_{2} V_{2}^{γ}

γ = \frac{C_{p}}{C_{V}} = \frac{5 / 2}{3 / 2} = 5 / 3

\frac{5 / 3}{1 - 5 / 3} = \frac{5 / 3}{2 / 3} = 5 / 2

γ - 1 = 2 / 3

d U = (C_{P} - P V^{α}) d T + V (ρ β - T_{α}) d P

d U = (\frac{5}{2} R - R) d T + V (1 - 1) d P = \frac{3}{2} R T

d S = \frac{C_{P}}{T} d T - V^{α} d P = \frac{5}{2} \frac{R}{T} d T - \frac{V}{T} d P

d S = \frac{5}{2} \frac{R}{T} d T - \frac{R}{P} d P

d S = \frac{C_{V}}{T} d T + \frac{α}{β} d V = \frac{3}{2} \frac{R}{T} d T + \frac{P}{T} d V = \frac{3}{2} \frac{R}{T} d T + \frac{R}{V} d V

Constant P:

Δ S = \frac{5}{2} R ln (\frac{T_{2}}{T_{1}})

Constant T:

Δ S = - R ln (\frac{P_{2}}{P_{1}})

Δ S = - R ln (\frac{V_{2}}{V_{1}})

Constant V:

Δ S = \frac{3}{2} R ln (\frac{T_{2}}{T_{1}})

Constant S:

\frac{P_{1}}{P_{2}} = {(\frac{T_{2}}{T_{1}})}^{5 / 2} = {(\frac{V_{1}}{V_{2}})}^{5 / 3}

d U = - P d V + T d S

d U = {(\frac{- \partial U}{\partial V})}_{S} d V + {(\frac{\partial U}{\partial S})}_{V} d S

\Rightarrow

{[\frac{\partial}{\partial S} (\frac{- \partial U}{\partial V})]}_{V} = {[\frac{\partial}{\partial V} {(\frac{\partial U}{\partial S})}_{V}]}_{S}

Note that these are second derivatives of the internal energy, so they should be negative for equilibrium.

8 Conditions for Equilibrium

Outcomes for this section:

Derive the condition for equilibrium between two phases.
Show that at constant temperature and pressure, the equilibrium state corresponds to that which minimizes the Gibbs free energy $G$ .
Explain why the evolution to a state of lower Gibbs free energy occurs spontaneously.

For an isolated system

(δ Q = 0, δ W = 0,

n fixed), equilibrium corresponds to the state of maximum entropy. So if we maximize

S

, which is a function of multiple variables, we will have determined the equilibrium state, regardless of the past history.

How do we recognize that a system has reached equilibrium? We need to be able to answer 'yes' to the following questions:

Is the system in a stationary state (i.e. not changing)?
If the system is isolated from its surroundings, will no further changes occur?

A useful example of the application of these systems is the copper rod in contact with hot and cold surfaces, shown in Figure 8.1. When the rod is first put into contact with the hot and cold surfaces, the system is clearly not in equilibrium because the temperature profile is changing and we answer 'no' to question 1. At long times a steady state temperature profile is reached, but the system is not at equilibrium because we would answer 'no' to question 2.

image: 20_home_ken_Mydocs_MSEcore_314_figures_Curod.svg

Figure 8.1: Illustration of a copper rod in contact with hot and cold surfaces. The temperature reaches a steady state profile at long times (

t = t_{\infty}

), but the system is not at equilibrium because the this temperature profile will change to a uniform value if the bar is isolated from its surroundings where it is no longer in contact with the hot and cold surfaces.

z varies monotonically with x,y - there is no global maximum. Constraints such as

y = y (x)

may define a maximum in

z (x, y)

subject to

y = y (x)

image: 21_home_ken_Mydocs_MSEcore_314_figures_3dplane.svg

Figure 8.2:

Example 5.1

z = x u + y v

For simple cases, eliminate dependent variables. In general, use Lagrange Multipliers.

Challenge: minimize a funciton of several variables when relationships (constraints) exist between those variables.

Approach: Lagrange Multipliers

\begin{matrix} \underline{Minimize: (will be S)} & \underline{Given these constraints (other state functions, vars)} \\ f (x_{1}, x_{2}, ... x_{n}) & Φ_{1} (x_{1}, x_{2}, ... x_{n}) = 0 \\ function of n variables & Φ_{2} (x_{1}, x_{2}, ...) = 0 \\ degrees of freedom=n-m & ⋮ \\ Φ_{m} (x_{1}, x_{2} ...) = 0 \end{matrix}

m constraints.

Define:

d f + λ_{1} d Φ_{1} + λ_{2} d Φ_{2} + ... + λ_{m} d Φ_{m} = 0

λ_{m} :

Lagrange multiplier

d F = \frac{\partial F}{\partial x_{1}} d x_{1} + \frac{\partial F}{\partial x_{2}} d x_{2} + ... + \frac{\partial F}{\partial x_{n}} d x_{n}

In general,

d F = \frac{\partial F}{\partial x_{1}} d x_{1} + \frac{\partial F}{\partial x_{2}} d x_{2} + ... + \frac{\partial F}{\partial x_{n}} d x_{n}

To guarantee that dF=0 for all

x_{1}, x_{2} ... x_{n}

, the coefficients

\frac{\partial F}{\partial x_{i}}

must all be zero.

i.e.

\frac{\partial F}{\partial x_{i}} + \sum_{k = 1}^{m} λ_{K} \frac{\partial Φ_{K}}{\partial x_{i}} = 0

Example 5.1

z = x u + y v

Constraints

$u = x + y + 12 \to Φ_{1} = x + y + 12 - u = 0$
$v = x - y - 8 \to Φ_{2} = x - y - 8 - v = 0$

u, v

: dependent

x, y

: independent

d z + λ_{1} d Φ_{2} + λ_{2} d Φ_{2} = 0

Minimize z subject to constraints

= x d u + u d x + y d v + v d y + λ_{1} (d x + d y - d u) + λ_{2} (d x - d y - d v) = 0

= (x - λ_{1}) d u + (y - λ_{2}) d v + (u + λ_{1} + λ_{2}) d x + (v + λ_{1} - λ_{2}) d y = 0

. \begin{matrix} x - λ_{1} = 0 \\ y - λ_{2} = 0 \end{matrix}} \Rightarrow \begin{matrix} λ_{1} = x \\ λ_{2} = y \end{matrix}

\begin{matrix} . \begin{matrix} u + λ_{1} + λ_{2} = 0 \\ v + λ_{1} - λ_{2} = 0 \end{matrix}} & \Rightarrow \begin{matrix} u = - λ_{1} - λ_{2} \\ v = - λ_{1} + λ_{2} \end{matrix} \Rightarrow \end{matrix}

\begin{matrix} u = - x - y \\ v = - x + y \end{matrix}

x + y + 12 - u = 0

\underline{x - y - 8 - v = 0}

\begin{matrix} 2 x + 4 - (- x - y) - (- x + y) = 0 & - 1 - y - 8 - (- (- 1) + y) = 0 \\ 4 x + 4 = 0 \Rightarrow x = - 1 & - 10 - 2 y = 0 \to y = - 5 \end{matrix}

8.1 Finding equilibrium conditions

A unary 2-phase system is in equilibrium when the

T, P

and

μ

for both phases are equal.

Consider 2 phases

α

and

β

of one component.

U = U^{α} + U^{β}

V = V^{α} + V_{β}

S = S^{α} + S^{β}

because these are extensive properties.

U^{α} (S^{α}, T_{α}, n_{α})

where

n_{α}

is the number of moles of

α

phase.

Then

d V^{α} = T_{α} d S^{α} - P_{α} d V^{α} + μ_{α} d n_{α}

, where

μ \equiv {(\frac{\partial V^{α}}{\partial n_{α}})}_{V_{α,} S^{α}}

μ_{α}

is the chemical potential of the

α

phase. To find the equilibrium condition, maximize S.

d S^{α} = \frac{d U α}{T_{α}} + \frac{P_{α}}{T_{α}} d V^{α} - \frac{μ_{α}}{T_{α}} d n_{α}

d S^{β} = \frac{d V_{β}}{T_{β}} + \frac{P_{β}}{T_{β}} d V_{β} - \frac{μ_{β}}{T_{β}} d n_{β}

d S = d S^{α} + d S^{β} = \frac{d U α}{T_{α}} + \frac{P_{α}}{T_{α}} d V^{α} - \frac{μ_{α}}{T_{α}} d n_{α} + \frac{d V_{β}}{T_{β}} + \frac{P_{β}}{T_{β}} d V_{β} - \frac{μ_{β}}{T_{β}} d n_{β}

If the entropy is maximized, then no changes will occur if the system is isolated (rigid walls, insulated).

d U = d U^{α} + d V_{β} = 0 \to d U^{α} = - d U^{β}

( no heat is exchanged)

d V = d V^{α} + d V_{β} = 0 \to d V^{α} = - d V_{β}

( no work is done)

d n_{α} = - d n_{β}

(particle number is conserved)

Then

d S = (\frac{1}{T_{α}} - \frac{1}{T_{β}}) d U^{α} + (\frac{P_{α}}{T_{α}} - \frac{P_{β}}{T_{β}}) d V_{β} - (\frac{μ_{α}}{T_{α}} - \frac{μ_{β}}{T_{β}}) d n_{α} = 0

To guarantee dS=0, these coefficients must be zero independently.

Hence,

\begin{matrix} T_{α} = T_{β}, P_{α} = P_{β}, μ_{A} = μ_{B} & Conditions for Equilibrium \end{matrix}

8.2 Energy Minima

Consider first the internal energy U in an m-component system.

d U = T d S + P d V + \sum_{i}^{m} μ_{i} d n_{i}

where

i :

index of components

d U = δ Q + δ W + δ W^{'}

Consider a reversible process in an isolated system

δ Q_{r e v} = T d S

δ W_{r e v} = - P d V

\Rightarrow

δ W^{'} = \sum_{i} μ_{i} d μ_{i}

“chemical” work associated with reversible reactions

Claim: For a system of constant

S, V, n_{λ}

, the equilibrium state is a state of minimum internal energy

U .

If this is not true, then work can be extracted and reinserted as heat. But then S would increase while nothing else changes. Therefore, energy cannot be extracted from a system under these conditions (unchanging/maximized

S_{v, n})

8.2.0.1 Derive conditions for equilibrium again

d U = 0

(minimize U)

d S = 0 \to

d S^{α} = - d S^{β}

d V = 0 \to

d V^{α} = - d V_{β}

d n = 0 \to

d n_{α} = - d n_{β}

d U^{α} = T_{α} d S^{α} - P_{α} d V^{α} + μ_{α} d n_{α}

\underline{d U^{β} = T_{β} d S^{β} - P_{β} d V_{β} + μ_{β} d n_{α}}

d U = (T_{α} - T_{β}) d S^{α} - (P_{α} - P_{β}) d V^{α} + (μ_{α} - μ_{β}) d n_{α} = 0

\Rightarrow T_{α} = T_{β}

P_{α} = P_{β}

μ_{α} = μ_{β}

(Additional condition: second derivative)

\Rightarrow

Thermal, mechanical, and chemical equilibrium

U will decrease spontaneously if a system of constant S and V is not in equilibrium.

Enthalpy

H = U + P V

Hemholtz Free Energy

F = U - T S

Gibbs Free Energy

G = U + P V - T S

The equilibrium conditions for different situations (constant

S

P

; constant

T,

V

; etc) are outlined below in table xx

Variables Held Constant	Equilibrium Condition
$S$ , $P$	$d H = 0$
$T$ , $V$	$d F = 0$
$T$ , $P$	$d G = 0$
$S$ , $V$	$d U = 0$

Table 2: Equilibrium conditions.

If T and P are held constant, a system will seek to minimize the Gibbs free energy,

G

. Consider two states connected by an isothermal and isobaric path:

G_{1} = U_{1} + P V_{1} - T S_{1}

G_{2} = U_{2} + P V_{2} - T S_{2}

Δ G = Δ U + P Δ V - T Δ S

, and

Δ U = Q + W + W^{'}

Consider first a reversible path:

W_{r e v, T} = - P Δ V

and

Q_{r e v, P} = T Δ S

For any path:

\begin{matrix} Δ G = [Q + W + W^{'}] - W_{r e v} - Q_{r e v} \\ Δ G = \underset{< 0}{\underset{⏟}{(Q - Q_{r e v})}} + \underset{< 0}{\underset{⏟}{(W - W_{r e v})}} + \underset{< 0}{W^{'}} \end{matrix}

In a system at constant T and P that is not in equilibrium, G will tend to decrease spontaneously to approach chemical equilibrium.

8.2.0.2 Example for two component system

Two isolated systems are defined - each in equilibrium with separate environments.

. \begin{matrix} P_{1} V_{1} = n_{1} R T_{1} \\ P_{2} V_{2} = n_{2} R T_{2} \end{matrix}}

Let them come to equilibrium in isolation

Δ U_{1} + Δ U_{2} = 0

\frac{3}{2} n_{1} R (T_{f} - T_{i}) + \frac{3}{2} n_{2} R (T_{f} - T_{i}) = 0

\Rightarrow n_{1} T_{f} - n_{1} T_{1} = - n_{2} T_{f} + n_{2} T_{2} \Rightarrow T_{f} = \frac{n_{1} T_{1} + n_{2} T_{2}}{n_{1} + n_{2}}

We can also solve for

P_{f}, V_{i}

P_{f} = \frac{(n_{1} + n_{2}) R T_{f}}{V_{1} + V_{2}} = \frac{R (n_{1} T_{1} + n_{2} T_{2})}{V_{1} + V_{2}}

and

V_{1} = \frac{n_{1} R T_{f}}{P_{f}}

V_{2} = \frac{n_{2} R T_{f}}{P_{f}}

V_{1} + V_{2} = \frac{n_{1} R T_{f}}{P_{f}} + \frac{n_{2} R T_{f}}{P_{f}}

\begin{matrix} P_{f} & V \\ n_{1} + n_{2} & T_{f} \end{matrix}

Final

8.3 Maxwell Relations

For free energies:

coefficients in opposite corners
derivatives in adjacent corners
minus signs apply to coeffiencients

For Maxwell Relations:

↶ = ↷

i.e.

- {(\frac{\partial S}{\partial P})}_{T} = {(\frac{\partial V}{\partial T})}_{P}

Note: This does not include the chemical potential.

δ W^{'} = \sum_{i}^{m} μ_{i} d n_{i}

8.3.0.1 Useful relations between S,T,P,V for an ideal monatomic gas

d S = \frac{C_{p}}{T} d T - V^{α} d P = \frac{5}{2} \frac{R}{T} d T - \frac{V}{T} d P = \frac{5}{2} \frac{R}{T} d T - \frac{R}{P} d P

d S = \frac{C_{V}}{T} d T + \frac{α}{β} d V = \frac{3}{2} \frac{R}{T} d T + \frac{P}{T} d V = \frac{3}{2} \frac{R}{T} d T + \frac{R}{V} d V

Constant P: {

Δ S = \frac{5}{2} R ln (\frac{T_{2}}{T_{2}})

Constant T:

{\begin{matrix} Δ S = - R ln (\frac{P_{2}}{P_{1}}) \\ Δ S = - R ln (\frac{V_{2}}{V_{1}}) \end{matrix}

Constant V:

Δ S = \frac{3}{2} R ln (\frac{T_{2}}{T_{1}})

Constant S:

\frac{P_{2}}{P_{1}} = {(\frac{T_{2}}{T_{1}})}^{5 / 2} = {(\frac{V_{1}}{V_{2}})}^{5 / 3}

image: 22_home_ken_Mydocs_MSEcore_314_figures_reverspath.svg

Figure 8.3:

d S = \frac{C_{v}}{T} d T + \frac{α}{β} d V = \frac{3}{2} \frac{R}{T} d T + \frac{P}{T} d V = \frac{3}{2} \frac{R}{T} d T + \frac{R}{V} d V

0 = \frac{3}{2} \frac{R}{T} d T + \frac{R}{V} d V

\to \frac{3}{2} ln (\frac{T_{2}}{T_{1}}) = - ln (\frac{V_{2}}{V_{1}})

{(\frac{T_{2}}{T_{1}})}^{3 / 2} = \frac{V_{1}}{V_{2}}

{(\frac{T_{2}}{T_{1}})}^{5 / 2} = {(\frac{V_{1}}{V_{2}})}^{5 / 3} = \frac{P_{2}}{P_{1}}

One can show this using

\frac{P_{1} V_{1}}{T_{1}} = \frac{P_{2} V_{2}}{T_{2}}

and substituting.

9 From Microstates to Entropy

Outcomes for this section:

Express the entropy $S$ of the system in terms of equivalent microstates in the equilibrium (most probable) macrostate.
Given the energy levels of a system of particles, calculate the partition function.
Given the partition function, calculate the Helmholtz free energy, the entropy, the internal energy, and the heat capacity.

Destination:

S = k_{B} ln Ω

where

k_{B} =

Boltzmann's constant,

8.317 \times 1 0^{- 5} e V / K, 1.38 \times 1 0^{- 23} J / K

and

Ω =

number of equivalent microstates in (equilibrium) macrostate.

Matter is composed of atoms, and is therefore discrete. Contimuum thermodynamics arises from interactions between discrete components and interactions with the environment.

A statistical description is needed to connect the microscopic and macroscopic descriptions.

9.1 Microstates and Macrostates

Microstate: Specification of the state (e.g. energy level) of every atom at a particular point in time.

Example: 4 identical particles in 2 levels, pour 4 balls in 2 boxes.

If balls are placed randomly, which configuration is more likely?

image: 23_home_ken_Mydocs_MSEcore_314_figures_microstates.svg

Figure 9.1:

# Microstates	Distribution
1	(4,0)
6	(2,2)
4	(1,3)

Table 3: Microstates and distribution of balls

Macrostate: collection of equivalent microstates. Equivalent means the same numbers of particles within each of the levels.

Example: the macrostate with 1L, 3R - (1,3)

We will use combinatorics to calculate:

image: 24_home_ken_Mydocs_MSEcore_314_figures_combin.svg

Figure 9.2: Macrostate (1,3)

The distribution function specifies the occupation of atomic states by identical particles, and thus the macrostate.
Number of macrostates $≪$ number of microstates
If all microstates are equally likely, then some macrostates are much more likely. (e.g. (2,2))

$\Rightarrow$ How do we see this?

9.1.0.1 How many microstates correspond to a given macrostate?

N_{0} :

# of balls,

r :

# of boxes,

n_{i} :

balls in

i^{t h}

box

\begin{matrix} Ω = \frac{N_{o}!}{n_{1}! n_{2}! n_{3}! ... n_{r}!} & n! \equiv n (n - 1) (n - 2) ...3 \cdot 2 \cdot 1 \\ = \frac{N!}{Π_{i = 1} n_{_{i}}!} \end{matrix}

Number of Microstates	Distribution
1	(4,0)	$Ω_{4, 0} = \frac{4!}{4! 0!} = 1$
6	(2,2)	$Ω_{2, 2} = \frac{4!}{2! 2!} = \frac{4 \cdot 3 \cdot 2 \cdot 1}{2 \cdot 1 \cdot 2 \cdot 1} = 6$
4	(1,3)	$Ω_{1, 3} = \frac{4!}{1! 3!} = \frac{4 \cdot 3 \cdot 2 \cdot 1}{1 \cdot 3 \cdot 2 \cdot 1} = 4$

Table 4: Microstates corresponding to given macrostates

Total number of possibilities is

r^{N_{o}}

, or

2^{4} = 16

. There are 5 macrostates: (4,0) (1,3) (2,2) (3,1) (4,0)

Example: Four atoms in volume V. How many microstates are there, and how many macrostates?

Divide each side into M compartments.
Compartments are so small that M $≫$ 4 and occupation is 0 or 1.

image: 25_home_ken_Mydocs_MSEcore_314_figures_gridstates.svg

Figure 9.3:

How many ways can we distribute 4 indistinguishable particles over 2M compartments?

Case I:

Ω_{I}

(\begin{matrix} 2 M \\ 4 \end{matrix}) = \frac{(2 M)!}{4! (2 M - 4)!} = \frac{2 M \cdot (2 M - 1) (2 M - 2) (2 M - 3)}{4!} \approx \frac{(2 M)^{4}}{4!}

Case II: How many configurations have all the particles on one side, i.e. M boxes?

Ω_{I I} = (\begin{matrix} M \\ 4 \end{matrix}) \approx \frac{M^{4}}{4!}

Note that

\frac{Ω_{I I}}{Ω_{I}} \approx \frac{1}{2^{4}} = \frac{1}{16}

Ω_{I I}

is much less likely.

For N atoms, we would find

\frac{Ω_{I I}}{Ω_{I}} = \frac{1}{2^{N}} ⋘ 1

Even a state with 51% on the left would be highly improbable.

\frac{(1.98 M)^{N}}{(2 M)^{N}}

for

N \sim N_{A}

is vanishingly small.( Try plotting this).

100 - 3.790

1000 -

4 \times 1 0^{- 5}

10000 -

2 \times 1 0^{- 44}

9.1.1 Postulate of Equal Likelihood

All allowable microstates (energetically equivalent configurations) are equally likely.

P_{j} = \frac{Ω_{j}}{r^{N_{o}}}

is the probability of finding the system in macrostate j. The most probable macrostate is the one that represents the most microstates in

Ω .

9.1.2 The Boltzmann Hypothesis (to be derived)

image: 26_home_ken_Mydocs_MSEcore_314_figures_boltzyo.svg

Figure 9.4:

S = k_{B} ln Ω

k_{B} = 1.38 \times 1 0^{- 23} J / K

Maximum in Ω corresponds to a maximum in S .

How do we determine the most probable macrostate?

What are the conditions of equilibrium?

9.2 Conditions for equilibrium

We aim to minimize

S

, where

S = k ln Ω

, or

S = k_{B} \underset{Ω}{\underset{⏟}{(\frac{N_{o}!}{Π_{i = 1}^{r} n_{i}!})}}

What tools do we need to do so?

ln (\frac{x}{y}) = ln x - ln y

ln (x y) = ln x + ln y

d ln x = \frac{d x}{x}

Stirling's Approximation:

ln x! ≊ x ln x - x

This is very accurate for large x. How large?

Express $Ω$ as a sum over logarithms of occupation numbers.

$Ω = \frac{N!}{Π_{i = 1}^{r} n_{i}!} \to ln Ω = ln N! - ln (Π_{i = 1}^{r} n_{i}!)$

Apply Stirling's Approximation, $ln (Π x_{i}) = \sum ln x_{i}$

$ln Ω = \approx N ln N - N - \sum_{i = 1}^{r} (n_{i} ln n_{i} - n_{i})$

Note also that $N = \sum_{i = 1}^{r} n_{i}$ (summing occupation numbers gives the total particle number).

So $ln Ω \approx N ln N - N - \sum_{i = 1}^{r} n_{i} ln n_{i} + N$

$= \sum_{i = 1}^{r} n_{i} ln N - \sum_{i = 1}^{r} n_{i} ln n_{i}$

$ln Ω \approx \sum_{i = 1}^{r} n_{i} (ln N - n_{i})$ Not too bad
Differentiate

$d ln Ω = \sum_{i = 1}^{r} [d n_{i} (ln N - ln n_{i}) + n_{i} (\frac{d N}{N} - \frac{d n_{i}}{n_{i}})]$

$= \sum_{i = 1}^{r} (ln N - ln n_{i}) d n_{i} + \underset{d N}{\underset{⏟}{\sum_{i = 1}^{r} (\frac{n_{i}}{N}) d N}} - \underset{d N}{\underset{⏟}{\sum_{i - = 1}^{r} d n_{i}}}$

$d ln Ω = - \sum_{i = 1}^{r} ln (\frac{n_{i}}{N}) d n_{i}$
Impose constraints

For an isolated system, the total particle number and energy are constant as $ln Ω$ is maximized.

$N = n_{1} + n_{2} + ... n_{r} = \sum_{i = 1}^{r} n_{i}$ , $d N = 0$

$U = n_{1} Σ_{1} + n_{2} Σ_{2} + ... + n_{r} Σ_{r} = \sum_{i = 1}^{r} n_{i} Σ_{i}$ , $d U = 0$

To impose constraints, we use Lagrange Multipliers.

$d ln Ω + λ_{1} d N + λ_{2} d U = 0$

$- \sum_{i = 1}^{r} ln (\frac{n_{i}}{N}) d n_{i} + λ_{1} \sum_{i = 1}^{r} d n_{i} + λ_{2} \sum_{i = 1}^{r} Σ_{i} d n_{i} = 0$

$- \sum_{i = 1}^{r} [ln (\frac{n_{i}}{N}) d n_{i} + λ_{1} - λ_{2} Σ_{i}] d n_{i} = 0$ $\Rightarrow$ Gives r equations, e.g.

$ln (\frac{n_{i}}{N}) - λ_{1} - λ_{2} Σ_{i} = 0 \to \frac{n_{i}}{N} = e^{λ_{1}} e^{λ_{2} Σ_{i}}$ , $i = 1, 2, ..., r$

Use constraints to eliminate $λ_{1},$ $λ_{2}$

\frac{n_{i}}{N} = e^{λ_{1}} e^{λ_{2} Σ_{i}}

\sum_{i = 1}^{r} \frac{n_{i}}{N} = 1 \to \sum_{i = 1}^{r} e^{λ_{1}} e^{λ_{2} Σ_{i}} = 1

e^{λ_{1}} = \frac{1}{\sum_{i = 1}^{r} e^{λ_{2} \sum_{i}}} \to \frac{n_{i}}{N} = \frac{e^{λ_{2} Σ_{i}}}{\sum_{j = 1}^{r} e^{λ_{2} Σ_{j}}} \equiv \frac{1}{Z} e^{λ_{2} Σ_{i}}

The fractional occupation number of the

i^{t h}

level.

ln Ω_{i} = - \sum_{i = 1}^{r} n_{i} (\frac{n_{i}}{N}) = - \sum_{i = 1}^{r} n_{i} ln (\frac{e^{λ_{2} Σ_{i}}}{Z})

= - \sum_{i = 1}^{r} n_{i} (λ_{2} Σ_{i} - ln Z)

ln Ω = - λ_{2} \sum_{i = 1}^{r} n_{i} Σ_{i} + ln Z \sum_{i = 1}^{r} n_{i} = - λ_{2} U + N ln Z

What is

λ_{2}

Consider response of system to the reversible absorption of an infinitesimal amount of heat

δ Q .

d ln Ω = - λ_{2} d U + d (N ln Z)

d U = δ Q_{r e v} = T d S

d ln Ω = - λ_{2} T d S

S \propto ln Ω

S = \underset{k_{B}}{\underset{⏟}{- \frac{1}{λ_{2} T}}} ln Ω = k_{B} ln Ω \to λ_{2} = - \frac{1}{k_{B} T}

\frac{n_{i}}{N} = \frac{e^{- Σ_{i} / k T}}{\sum_{i = 1}^{r} e^{- Σ_{i} / k T}} \equiv \underset{}{\underset{⏟}{\frac{1}{Z}}} \underset{}{\underset{⏟}{e^{- Σ_{i} / k T}}}

We can calculate macroscopic properties from the partition function.

Recall

ln Ω = - λ_{2} U + N ln Z,

S = k ln Ω

(k ln Ω =)

S = - \frac{U}{T} + k_{B} N ln Z

- k T ln Z = U - T S \equiv F

Hemholtz Free Energy!

F = - k T N ln Z

\frac{F}{N} = - k T ln Z

Also,

S = - {(\frac{\partial F}{\partial T})}_{V} = N k ln Z + N k T {(\frac{\partial ln Z}{\partial T})}_{V}

Then

U = F + T S = N k T^{2} {(\frac{\partial ln Z}{\partial T})}_{V}

C_{V} = {(\frac{\partial U}{\partial T})}_{V} = 2 N k T {(\frac{\partial ln Z}{\partial T})}_{V} + N k T^{2} {(\frac{\partial^{2} ln Z}{\partial T^{2}})}_{V}

Note that the pressure dependence of

Z

is needed to calculate

V, H, G, C_{P} .

10 Noninteracting (Ideal) Gas

The definition of an ideal gas is that there are no interactions between the molecules, they only have kinetic energy. The total kinetic energy for an ideal gas of molecules, each with mass,is as follows:

\begin{matrix} \sum \frac{1}{2} m v^{2} = \sum \frac{m}{2} (v_{x}^{2} + v_{y}^{2} + v_{z}^{2}) & (10.1) \end{matrix}

The energy distribution of free particles is continuous.

$\sum \to \int$
For convenience, assume box of dimensions $L \times L \times L = V$

Z = \underset{V}{\underset{⏟}{\int_{0}^{L} \int_{0}^{L} \int_{0}^{L}}} d x d y d z \int_{- \infty}^{\infty} \int_{- \infty}^{\infty} \int_{- \infty}^{\infty} e^{- \frac{1}{2 k T} (v_{x}^{2} + v_{y}^{2} + v_{z}^{2})} ⅆ v_{x} ⅆ v_{y} ⅆ v_{z}

= V \int_{- \infty}^{\infty} e^{\overset{Gaussians}{\overset{⏞}{- \frac{1}{2 k T} m v_{x}^{2}}}} ⅆ v_{x} \int_{- \infty}^{\infty} e^{- \frac{1}{2 k T} m v_{y}^{2}} d v_{y} \int_{- \infty}^{\infty} e^{- \frac{1}{2 k T} m v_{Z}^{2}} ⅆ v_{z}

\int_{- \infty}^{\infty} e^{- α x^{2}} ⅆ x = \sqrt{\frac{π}{α}}

(for

α > 0

)

e^{\overset{α}{\overset{⏞}{- \frac{1}{2 k T} m}} v_{x}^{2}}

∴ Z = V {(\frac{2 π k T}{m})}^{3 / 2}

Now we can easily derive many functions.

ln Z = ln V + \frac{3}{2} ln (\frac{2 π k}{m}) + \frac{3}{2} ln T

\frac{\partial ln Z}{\partial T} = \frac{3}{2} \frac{1}{T}

\Rightarrow F = - N k T ln Z = - N k T [ln V + \frac{3}{2} ln (\frac{2 π k T}{m})]

U = N k T^{2} {(\frac{\partial ln Z}{\partial T})}_{V} = N k T^{2} (\frac{3}{2} \frac{1}{T}) = \frac{3}{2} N k T

\begin{matrix} \frac{U}{N} = \frac{3}{2} kT & Energy per particle \end{matrix}

C_{V} = {(\frac{\partial U}{\partial T})}_{V} = \frac{3}{2} N K = \frac{3}{2} (\frac{N}{N_{A}}) k N_{A} = \frac{3}{2} n R

\begin{matrix} \frac{C_{V}}{n} = \frac{3}{2} R & n: moles \end{matrix}

10.1 Ideal gas Law

d F = - S d T - P d V + δ W^{'}

- P = {(\frac{\partial F}{\partial V})}_{T}

P = - N k T {(\frac{\partial ln Z}{\partial V})}_{T} = N k T {[\frac{\partial}{\partial V} (ln V + \frac{3}{2} ln (\frac{2 π k}{m}) + \frac{3}{2} ln T)]}_{T}

P=NkT \cdot \frac{1}{V} = \frac{nRT}{V}

Note that we have ignored interactions between particles/atoms. Attractive interactions lead to, e.g. condensation.
We have also ignored repulsive interactions, i.e. atoms occupy finite volumes.

Including these leads to the van der Waals equation:

(P + \frac{a}{V^{2}}) (V - b) = R T

11 Diatomic Gases

Diatomic gases possess rotational and vibrational degrees of freedom.

The kinetic energy of a gas molecule with p degrees of freedom is

Σ = \sum_{j = 1}^{P} b_{j} v_{j}^{2}

, and

Z = V Π_{j = 1}^{P} \sqrt{\frac{π k T}{b_{j}}}

(e.g.

b = \frac{m}{2}

for translations) For rotations

v \to ω

M \to I

Surprisingly,

U

and

C_{V}

do not depend on

b_{j}

{(\frac{\partial ln Z}{\partial T})}_{V} = \frac{P}{2 T} \to U = N k T^{2} (\frac{P}{2 T}) = \frac{P}{2} N k T

Get

\frac{1}{2} R T

for each degree of freedom

C_{V} = \frac{P}{2} N k = \frac{P}{2} n R

Observations:

Heat capacity measurement reveals the number of degrees of freedom.

Monatomic: 3 translational
Heteronuclear Diatomic: 3 translational + 2 rotational + 2 vibrational

image: 27_home_ken_Mydocs_MSEcore_314_figures_diatomic.svg

Figure 11.1: Diatomic gas

12 The Einstein Model of a Crystal

How is the discrete nature of matter manifested in easily observable quantities?

Consider atoms in a simple cubic lattice

Bounded to six nearest neighbors (vibrating in harmonic potential) $F = - k x$ , $ω = \sqrt{\frac{k}{m}}$

image: 28_home_ken_Mydocs_MSEcore_314_figures_einstein1.svg

Figure 12.1: Vibration of atoms in harmonic potential

3 bonds/atom, 3N bonds in crystal

Figure 12.2: Binding to six nearest neighbors

By solving the Schrödinger equation for the harmonic oscillator potential, one can show that

\sum_{i} = (i + \frac{1}{2}) ℏ ω = (i + \frac{1}{2}) h v

i = 0, 1, 2...

h

: Planck's constant ,

v :

frequency ,

ℏ : \frac{h}{2 π}

Energy is stored in vibration of atoms. To analyze, calculate the partition function for the vibrations:

Z = \sum_{i = 0}^{n} e^{- Σ_{i} / k T} = \sum_{i = 0}^{n} e^{- (i + \frac{1}{2}) h v / k T} = e^{- \frac{1}{2} \frac{h v}{k T}} \sum_{i = 0}^{n} e^{- i h v / k T}

Here n is the number of energy levels. If n is large, we can take the limit

n \to \infty

and use

∴

\sum_{i = 0}^{\infty} e^{- i h v / k T} = \frac{1}{1 - e^{- h v / k T}}

Z = \frac{e^{- 1 / 2 \frac{h v}{k T}}}{1 - e^{- h v / k T}}

12.1 Thermodynamic Properties of a Crystal

Vibrations along each of three bonding axes contribute to energy:

F = - 3 N k T ln Z = 3 N k T [\frac{h v}{2 k T} + ln (1 - e^{- h v / k T})]

= \frac{3}{2} N h v + 3 N k T ln (1 - e^{- \frac{h v}{k T}})

Note that the crystal has energy even at zero T!

U = - \frac{\partial}{\partial β} ln Z = k T^{2} \frac{\partial ln Z}{\partial T}

(

β = k T)

(per particle?)

U = 3 N k T^{2} \frac{\partial ln 2}{\partial T} = 2 N k T^{2} \frac{\partial}{\partial T} [- \frac{1}{2} \frac{h v}{k T} - ln (1 - e^{- h v / k T})]

U = \frac{3}{2} N h v [\frac{1 + e^{- h v / k T}}{1 - e^{- h v / k T}}]

How does this change with temperature?

The heat capacity,

C_{V} = \frac{\partial U}{\partial T}

C_{V} = \frac{3}{2} N h v \cdot \frac{h v}{k T^{2}} e^{- h v / k T} \times \frac{(1 - e^{- h v / k T}) + (1 + e^{- h v / k T})}{(1 - e^{- h v / k T})^{2}}

C_{V} = 2 N k {(\frac{h v}{k T})}^{2} \frac{e^{- h v / k T}}{(1 - e^{- h v / k T})^{2}}

image: 29_home_ken_Mydocs_MSEcore_314_figures_cvgraph.svg

Figure 12.3: Heat capacity in an atom as a function of temperature

Classical limit

(3 R \frac{J}{m o l - K})

The Einstein model captures the qualitative behavior of the heat capacity very well. (But something is missing).

Note here regarding information derived from heat capacity.

13 Unary Heterogeneous Systems

Outcomes for this section:

State the differential of the Gibbs free energy $G$ as a function of $S$ , $T$ , $V$ , and $P$ .
State the conditions for two phases to coexist in equilibrium.
Explain how isobaric section of the chemical potential $μ (T, P)$ as a function of temperature and pressure can be calculated from knowledge of the heat capacity and the entropy at room temperature.
Given $μ (T, P)$ for multiple phases, determine the equilibrium phase at a given temperature.
Derive the Clausius-Clapeyron relation: express the general condition for determining the region of two-phase coexistence.
Calculate the $Δ H$ given the $C_{P} (T)$ , assuming a negligible contribution from thermal expansion.
Calculate $Δ V^{α \to β}$ assuming ideal gas behavior.
Integrate $\frac{d P}{d T} = \frac{Δ S}{Δ V}$ with the assumption that $Δ S$ and $Δ V$ depend only weakly on the temperature.
Given the $P - T$ diagram, qualitatively sketch $G (T)$ for a specified region.
Given the $P - T$ diagram, specify the sign of $Δ V^{α \to β}$ .
State Trouton's rule and justify its validity qualitatively.
Sketch the $P - T$ diagram for a one-component system.

Unary material: single chemical component
Homogeneous: 1 phase
Heterogeneous: 2 phase
Phases: Gas, Liquid, Solid; allotropes are distinct solid phases
Phase boundary: limit of phase stability
- multiple phases co-exist in equilibrium at a phase boundary
- Boundary defined by Clasius - Clapeyron Equation
Phase transformation: solid $\to$ liquid, liquid $\to$ vapor, allotropic process of phase transformation determines microstructure

13.1 Phase Diagrams

Phase Diagram of Unary Heterogeneous System

image: 30_home_ken_Mydocs_MSEcore_314_figures_phasediagcuu.svg

Figure 13.1: Phase Diagram Cu.

Phase $\to$ solid, liquid, gas regions
Unary $\to$ single component
Heterogeneous $\to$ more than one phase
(Cu) $\to$ component

The phase boundary defines the limits of phase stability. Phases co-exist at a phase boundary. A phase transformation occurs when crossing phase boundaries i.e.

s \to ℓ, ℓ \to v, s \to v

image: 31_home_ken_Mydocs_MSEcore_314_figures_phasediagc.svg

Figure 13.2: Phase Diagram of Unary Heterogeneous System (C)

image: 32_home_ken_Mydocs_MSEcore_314_figures_phasediagh20.svg

Figure 13.3: Componds can be treated as unary systems

(H_{2} O)

13.2 Chemical Potential Surfaces

To find

μ (T, P)

, integrate

d μ = d G = - S d T + V d P

knowns:

C_{P}

, expansion coefficient, compressibility depends on phase

Then repeat for each phase (solid

α,

solid

β

, liquid, etc. )

image: 33_home_ken_Mydocs_MSEcore_314_figures_chempot1.svg

image: 34_home_ken_Mydocs_MSEcore_314_figures_chempot2.svg

Figure 13.4: Solid

α

and liquid L

μ^{L} (T, P)

and

μ^{S} (T, P)

(two surfaces) intersect at a line defined by

μ^{L} = μ^{S} .

image: 35_home_ken_Mydocs_MSEcore_314_figures_gbsurface.svg

Figure 13.5: Intersection of

μ^{L} (T, P)

and

μ^{S} (T, P)

$μ^{L}$ and $μ^{S}$ must be computed from same reference state (e.g. $μ^{S} (T_{o}, ℓ_{o})$
Equilibrium conditions are met at intersection
$T^{α} = T^{L},$ $P^{α} = P^{L}$ , $μ^{α} = μ^{L}$

image: 36_home_ken_Mydocs_MSEcore_314_figures_superpos.svg

Figure 13.6: Superposition of Solid, Liquid, and Gas phase

μ

ℓ

Relation between chemical potential and the Gibb's free energy (for unary systems).

G: intensive molar Gibbs free enrgy

G^{'} = n G :

Extensive

d U^{'} = T d S^{'} - P d V^{'} + μ d n_{1}

μ = {(\frac{\partial u^{'}}{\partial n})}_{S^{'}, V^{'}}

G^{'} = U^{'} + P V^{'} - T S^{'}

d G^{'} = d U^{'} + P d V^{'} + V^{'} d P - T d S^{'} - S^{'} d T

Susbstitute

d U^{'}

d G^{'} = T d S^{'} - P d V^{'} + μ d n + P d V^{'} + V^{'} d P - T d S^{'} - S^{'} d T

d G^{'} = - S^{'} d T + V^{'} d P + μ d n

μ = {(\frac{\partial G^{'}}{\partial n})}_{T, P}

μ = {(\frac{\partial G^{'}}{\partial n})}_{T, P} = {(\frac{\partial}{\partial n} (n G))}_{T, P} = G {(\frac{\partial}{\partial n})}_{T, P} = G

13.3 $μ (T, P)$ Surfaces

d μ^{α} = d G^{α} = - S^{α} d T + V^{α} d P

Approach: compute isobaric sections by integrating

- S^{α} d T

d S_{P}^{α} = \frac{C_{P}^{α}}{T} d T \Rightarrow S^{α} (T) = S^{α} (298) + \int_{298}^{T} \frac{C_{P}^{α} (T^{'})}{T^{'}} ⅆ T^{'}

μ^{α} (T) = μ^{α} (298) - \int_{298}^{T} S^{α} (T^{'}) ⅆ T^{'}

μ^{α} (T) = μ^{α} (298) - \int_{298}^{T} [S^{α} (298) + \int_{298}^{T "} \frac{C_{P}^{α} (T^{'})}{T} ⅆ T^{'}] ⅆ T "

To compare

μ^{α}

with

μ^{L}

, we need to calculate

μ^{L}

from the same reference point.

Connecitng

μ^{α}

with

μ^{L}

at the melting point

T_{m} :

μ^{L} (T) - μ^{α} (298) = \underset{}{\underset{⏟}{[μ^{L} (T) - μ^{L} (T_{m})]}} + \underset{}{\underset{⏟}{[μ^{α} (T_{m}) - μ^{α} (298)]}}

μ^{L} = μ^{L} (T_{m}) - \int_{T_{M m}}^{T} [S^{L} (T_{m})^{*} + \int_{T_{m}}^{T "} \frac{C_{P}^{L} (T^{'})}{T^{'}} ⅆ T^{'}] ⅆ T "

Plot

G (T) - G^{α} (298)

versus T for each phase

α, L

i.e. plot of

G^{α}

begins at 0, do example where P=1 bar.

* Note the entropy changes with the phase change

S^{L} (T_{m}) = S^{α} (T_{m}) + Δ S^{α \to L} (T_{m})

Δ S :

latent heat

S^{L} (T_{m}) = \underset{S_{298}^{α} + \int_{298}^{T_{m}} \frac{C_{P}^{α} (T) d T}{T}}{\underset{⏟}{S^{α} (T_{m})}} + \underset{latent heat}{\underset{⏟}{Δ S^{α \to L} (T_{m})}}

G^{L} (T) - G^{α} (298) = G^{L} (T) - G^{L} (T_{m}) + G^{α} (T_{m}) - G^{α} (298) =

= \int_{T_{m}}^{T} - {[\underset{S^{L} (T_{m})}{\underset{⏟}{\overset{S^{α} (T_{m})}{\overset{⏞}{S^{α} (298 + \int_{298}^{T_{m}} \frac{C_{P}^{α} (T^{'})}{T^{'}} ⅆ T^{'}}} + Δ S^{α \to L} (T_{m})}}] + \underset{\frac{C_{P}^{L} (T^{'})}{T^{'}}}{\int_{T_{m}}^{T "}}}

+ (-) \int_{298}^{T_{m}} [S^{α} (298) + \int_{298}^{T "} \frac{C_{P}^{α} (T)}{T^{'}} ⅆ T^{'}] ⅆ T "

image: 37_home_ken_Mydocs_MSEcore_314_figures_deteqstate.svg

Figure 13.7: Determining the equilibrium state (at fixed P)

13.4 Clasius-Clapeyron Eq.

Goal: Determine two-phase coexistence lines in order to complete the P-T phase diagram

Areas: single phase

Lines: 2-phase

Intersections: 3 phases (triple point)

Consider co-existence of two phases in equilibrium:

T^{α} = T^{β}

P^{α} = P^{β}

μ^{α} = μ^{β}

Phase changes change the amounts of two phases:

d μ^{α} = - S^{α} d T^{α} + V^{α} d P^{α}

d μ^{β} = - S^{β} d T^{β} + V^{β} d P^{β}

But we require equilibrium:

\begin{matrix} d T^{α} = d T^{β} & d P^{α} = d T^{β} & d μ^{α} = d μ^{β} \end{matrix}

- S^{α} d T + V^{α} d P = - S^{β} d T + V^{β} d P

(S^{β} - S^{α}) d T = (V^{β} - V^{α}) d P

Δ S^{α \to β} d T = Δ V^{β \to α} d P

Δ S^{α \to β} :

difference in molar entropy

Δ V^{α \to β}

: difference in molar volume

\begin{matrix} \frac{dP}{dT} = \frac{Δ S^{α \to β}}{Δ V^{α \to β}} & Classius-Claperyon Equation \end{matrix}

Slope =

\frac{Entropy Change}{Volume Change}

But how do we measure entropy change?

Instead, we measure the heat of fusion of vaporization isobarically under reversible conditions.

So,

Q^{α \to β} = Δ H^{α \to β}

In equilibrium,

\begin{matrix} G^{α} = G^{β} & H^{α} - T S^{α} = H^{β} - T S^{β} & (T^{α} = T^{β} \end{matrix}

Δ S^{α \to β} = \frac{Δ H^{α \to β}}{T}

, and

\frac{d P}{d T} = \frac{Δ H^{α \to β}}{T Δ V^{α \to β}}

Can be integrated to get

P (T)

for 2-phase coexistence.

We need

Δ H (P, T)

Δ V (P, T)

from Chapter 4.

13.4.1 Step 1: Find $Δ H (T, P)$

d (Δ H^{α \to β}) = d (H^{β} - H^{α}) = d H^{β} - d H^{α}

d H = C_{P} d T + V (1 - T_{α}) d P

d Δ H^{α \to β} = Δ C_{P} d T + \underset{}{\underset{⏟}{Δ [V (1 - T_{α}) d P}}

To find

Δ H

, we need the temperature dependence of the heat capacity.

C_{P} (T)

is often given empirically as

C_{P} = a + b T + \frac{c}{T^{2}} + d T^{2}

(See Appendix B,E)

Δ C_{P} = Δ a + Δ b T + \frac{Δ c}{T^{2}} + Δ d T^{2}

Now we can integrate to get

Δ H .

13.4.2 Step 2: Find $Δ V^{α \to β} (T, P) \equiv V^{β} (P, T) - V^{α} (P, T)$

First consider the case of

β

as a vapor phase, and

α

as liquid or solid.

$V^{β} ≫ V^{α}$
Assume ideal gas behaviour.

Δ V^{α \to β} = V^{β} - V^{α} \approx V^{β} = \frac{R T}{P}

Then for sublimation or vaporization to phase

β

\frac{d P}{d T} = \frac{Δ H^{α \to β}}{T Δ V^{α \to β}} = \frac{Δ C_{P} d T}{T \cdot \frac{R T}{P}} = Δ C_{P} \frac{P}{R T^{2}} d T

small, positive slope

Phase boundaries can be calculated based on knowledge of

C_{P} .

(or vice versa, as we will see)

For solid

\to

solid transformations, (

β

is the stable phase at high T)

\frac{d P}{d t} = \frac{\overset{}{\overset{⏞}{Δ C_{P}^{α \to β} (T)}} d T}{\underset{}{\underset{⏟}{T Δ V}}}

Δ V

is usually positive but can be negative (e.g.

H_{2} O

)

Δ V

~ constant over few 10's of atmosphere.

An approximate analysis of solid-solid phase boundary:

Δ S, Δ H, Δ V

are determined by

C_{P}, α, β

, but suppose the variation with temperature is weak.

Since

\frac{d P}{d T} = \frac{Δ S}{Δ V} = constant

P - P_{o} \approx \frac{Δ S}{Δ V} (T - T_{o}) \approx \frac{Δ H}{Δ V} (\frac{T - T_{o}}{T_{o}})

The slope

\frac{d P}{d T}

is generally large since

Δ V

is small.

image: 38_home_ken_Mydocs_MSEcore_314_figures_logPgraph.svg

Figure 13.8:

\frac{d P}{d T} \approx \frac{Δ H}{T Δ V} \approx \frac{Δ H}{R T^{2}} \cdot P

\frac{d P}{P} \approx \frac{Δ H (T)}{R T^{2}} d T

If we assume

\frac{d}{d T} Δ H = 0

ln (\frac{P}{P_{o}}) = - \frac{Δ H}{R} (\frac{1}{T} - \frac{1}{T_{o}})

{| \frac{d P}{d T} |}^{S \to L} > {| \frac{d P}{d T} |}^{S \to V}

13.4.3 Justification for Approximations

Consider the enthalpy of transformation

d Δ H^{α \to β} (T) = Δ C_{p} (T) d T

, and integrate

Δ H (T) = \underset{}{\underset{⏟}{Δ H (T_{o})}} + \underset{}{\underset{⏟}{\int_{T_{o}}^{T} Δ C_{P} (T) ⅆ T}}

Δ H (T_{o})

: enthalpy change at the transformation temperature.

Heat to drive phase change is larger than that needed to change the temperature.

Thus,

Δ H (T) \approx Δ H (T_{o})

For vaporization,

ln (\frac{P}{P_{o}}) \approx - \frac{Δ H (T_{o})}{R} (\frac{1}{T} - \frac{1}{T_{o}})

13.4.4 Trouton's Rule

Δ S_{v a p}

is approximately the same for all materials.

Δ S = \frac{Δ H}{T} \to

materials with high boiling points have larger

Δ H_{v a p} .

ln (\frac{P}{P_{o}}) = - (\frac{Δ H}{R}) \frac{1}{T} + (\frac{Δ H}{R T_{o}})

image: 39_home_ken_Mydocs_MSEcore_314_figures_tempgraph.JPG

Figure 13.9:

14 Open Multicomponent Systems

Outcomes for this section:

Given sufficient information about the dependence of a total property $B$ or $Δ B$ versus composition, find the partial molal properties as a function of composition via calculations of derivatives $d B$ or $d Δ B$ .
Given the partial molal properties as a function of composition, calculate the total properties of the system via integration of the derivatives.
Given the differentials of state functions, write partial derivatives that define the partial molal properties.
What is $B_{k}^{0}$ ?
What is $μ_{k} - μ_{k}^{0}$ for (a) a component behaving ideally, and (b) in general?
Define the activity of a component.
Given $μ_{k} (T, P, X_{k})$ , calculate changes in the partial molal properties.
State and justify/explain Raoult's law.
State and justify/explain Henry's law.
Explain how the activity coefficient $γ$ can be used to describe the departure from ideal behavior in terms of ``excess'' quantities.
Define a ``regular'' solution and calculate the partial molal properties and total properties versus composition for binary mixtures.
Describe the driving forces for mixing and their origins in statistical mechanics.
Interpret changes in state functions with mixing in terms of ideal behavior and departures from ideality.

14.1 Partial Molal Properties of Open Multicomponent Systems

Volume

V^{'}

is an extrinsic quantity that depends on amount of each component:

V^{'} = V^{'} (T, P, n_{1}, n_{2}, ... n_{c})

\begin{matrix} C : # components & x_{c} : mole fraction & n_{k} : # moles of component k \end{matrix}

Then

d V^{'} = {(\frac{\partial V^{'}}{\partial T})}_{P, n_{m}} d T + {(\frac{\partial V^{'}}{\partial P})}_{T, n_{k}} d P + \sum_{k = 1}^{c} {(\frac{\partial V^{'}}{\partial n_{k}})}_{T, P, n_{o} \neq n_{k}} d n_{k}

We previously defined coefficients of

d P, d T

For convenience, define

{\overline{V}}_{K} \equiv {(\frac{\partial V^{'}}{\partial n_{k}})}_{T, P, n_{j} \neq n_{k}}

as partial molal volumes.

We can do the same for any other extensive property

B^{'} (U^{'}, S^{'}, F^{'}, G^{'}, H^{'})

d B^{'} = M d T + N d P + \sum_{k = 1}^{r} {\overline{B}}_{k} d n_{k}

{\overline{B}}_{K} \equiv {(\frac{\partial B^{'}}{\partial n_{k}})}_{T, P, n_{j} \neq n_{k}}

k = 1, 2, > ... <

Consider a system (or sample) that we create by adding various amounts of the components sequentially (holding others constant).

d T = d P = 0,

d K_{T, P}^{'} = \sum_{k = 1}^{C} {\overline{V}}_{k} d n_{k}

, which we could integrate.

But

{\overline{V}}_{k}

depends on the composition, which changes continuously.

However, we can calculate changes in state functions using the simplest possible path: add all components simultaneously and in the proportions of the final mixture.

\to

Intensive properties

(T, P, X_{k})

are constant

V^{'} = \sum_{k = 1}^{C} {\overline{V}}_{k} d n_{k} = \sum_{k = 1}^{C} {\overline{V}}_{k} \int_{0}^{n_{k}} ⅆ n_{k} = \sum_{k = 1}^{C} {\overline{V}}_{k} n_{k}

and

B^{'} = \sum_{k = 1}^{C} {\overline{B}}_{k} n_{k}

Interpretation: We can calculate how much each component contributes to a given extensive quantity.

14.2 Gibbs - Duhem Equation: Evaluating Differentials

d B^{'} = d [\sum_{k = 1}^{C} ({\overline{B}}_{k} n_{k})] = \sum_{k = 1}^{c} d ({\overline{B}}_{k} n_{k})

Apply product rule:

d B^{'} = \sum_{k = 1}^{C} {\overline{B}}_{k} d n_{k} + \sum_{k = 1}^{C} n_{k} d {\overline{B}}_{k},

but

d P, d T

are held constant, and

d B^{'} = \underset{0}{\underset{⏟}{M d T + N d P}} + \sum_{k = 1}^{C} {\overline{B}}_{k} d n_{k}

\to \sum_{k = 1}^{C} n_{k} d {\overline{B}}_{k} = 0

Gibbs Duhem equation relates the different partial molal properties. To be shown: given one, the others can be computed. For two components:

n_{1} d {\overline{B}}_{1} + n_{2} {\overline{B}}_{2} = 0

14.3 The Mixing Process: Calculating changes in energy

image: 40_home_ken_Mydocs_MSEcore_314_figures_mixing.svg

Figure 14.1: Mixing of three states into

B_{s o ln}

Reference and Final States have the same T and P.

B_{k}^{o} :

value of property B for pure component, per mole.

B^{'}^{o} = \sum_{k = 1}^{C} B_{k}^{o} n_{k}

: total value of B

Δ B_{m i x}^{'} - B_{s o ln}^{'} - B^{'}^{o}

Δ B_{m i x}^{'} = \sum_{k = 1}^{C} {\overline{B}}_{k} n_{k} - \sum_{k = 1}^{C} B_{k}^{o} n_{k} = \sum_{C = 1}^{k} \overset{Δ {\overline{B}}_{k}}{\overset{⏞}{({\overline{B}}_{k} - \dot{B_{k})}}} n_{k}

Δ B_{m i x}^{'} = \sum_{k = 1}^{C} Δ {\overline{B}}_{k} n_{k}

per mole

Δ B = \frac{Δ B^{'}}{n_{T}} = \sum_{k = 1}^{C} Δ {\overline{B}}_{k} \frac{n_{k}}{n_{T}} = \sum_{k = 1}^{C} Δ {\overline{B}}_{k} X_{k}

How does this vary with changes in composition?

Δ B_{m i x}^{'} = \sum_{k = 1}^{C} Δ {\overline{B}}_{k} n_{k}

d (Δ B^{'}) = \sum_{k = 1}^{C} ({\overline{B}}_{k} d n_{k} - B_{n}^{o} d n_{k}) = \sum_{k = 1}^{C} Δ {\overline{B}}_{k} d n_{k}

Alternatively, we could have written

d (Δ B^{'}) = \sum_{k = 1}^{C} (Δ \overline{B} d n_{k} + n_{k} d Δ {\overline{B}}_{k}) \to \sum_{k = 1}^{C} n_{k} d Δ {\overline{B}}_{k} = 0

We can also express these per mole:

d Δ B_{m i x} = \sum_{k = 1}^{C} Δ {\overline{B}}_{k} d X_{k}

\sum_{k = 1}^{C} X_{k} d Δ {\overline{B}}_{k} = 0

How do we find molal properties?

Measurement of total property B or $Δ B$ versus composition.
Measurements of PMP ${\overline{B}}_{k}$ versus composition.

We will first apply to two component systems.

B = {\overline{B}}_{1} x_{1} + {\overline{B}}_{2} x_{2}

d B = {\overline{B}}_{1} d x_{1} + {\overline{B}}_{2} x_{2}

d x_{1} = - d x_{2}

x_{1} + x_{2} = 1

x_{2} = 1 - x_{1}

d B = ({\overline{B}}_{1} - {\overline{B}}_{2}) d X_{1}

\frac{d B}{d X_{1}} = {\overline{B}}_{1} - {\overline{B}}_{2}

B = {\overline{B}}_{1} x_{1} + ({\overline{B}}_{1} - \frac{d B}{d X_{1}}) (1 - X_{1}) = {\overline{B}}_{1} - \frac{d B}{d X_{1}} + \frac{d B}{d X_{1}} X_{1}

Solve for

{\overline{B}}_{1}

{\overline{B}}_{1} = B + (1 - X_{1}) \frac{d B}{d X_{1}}

and

{\overline{B}}_{2} = B + (1 - X_{2}) \frac{d B}{d X_{2}}

Note also that

Δ B_{1} = Δ B + (1 - X_{1}) \frac{d Δ B}{d X_{1}}

;

Δ B_{2} = Δ B + (1 - X_{2}) \frac{d Δ B}{d X_{2}}

from Daltoff 8.2.1

Problem 8.3: Given behavior of volume change upon mixing

Δ V_{m i x} = 2.7 X_{1} X_{2}^{2}

(L ? ? / m o l)

, derive expressions for partial molal volumes of each component as a function of composition.

Δ V_{m i x} = 2.7 X_{1} X_{2}^{2} = a X_{1} X_{2}^{2}

a = 2.7

To take derivative, express in terms of

X_{2}

Δ V_{m i x} = a (1 - X_{2}) X_{2}^{2}

\frac{d Δ V_{m i x}}{d X_{2}} = 2 a X_{2} - 3 a X_{2}^{2} = - \frac{d Δ V_{m i x}}{d X_{1}}

Now use relations derived in lecture:

Δ {\overline{B}}_{1} = Δ B_{m i x} + (1 - X_{1}) \frac{d Δ B_{m i x}}{d X_{1}}

(B \to V)

14.4 Graphical Determination of Partial Molal Properties

Δ {\overline{B}}_{2} = Δ B_{m i x} + (1 - X_{2}) \frac{d Δ B_{m i x}}{d X_{2}}

Δ {\overline{B}}_{2} = A B + P B \cdot \frac{B C}{P B} = A B + B C = A C

image: 41_home_ken_Mydocs_MSEcore_314_figures_graphdet.svg

Figure 14.2:

Evaluations of PMPs: given

{\overline{B}}_{1} (X) \to {\overline{B}}_{2} (X_{1})

B

Gibbs - Duhem:

X_{1} d {\overline{B}}_{1} + X_{2} d {\overline{B}}_{2} = 0

d {\overline{B}}_{1} = - \frac{X_{2}}{X_{1}} d {\overline{B}}_{2}

{\overline{B}}_{1} = {\overline{B}}_{1} (x = 0) + \int_{0}^{X_{2}} ⅆ {\overline{B}}_{1} = B_{1}^{0} + \int_{0}^{X_{2}} (\frac{- X_{2}}{X_{1}} d {\overline{B}}_{2})

d {\overline{B}}_{2} = \frac{d \overline{B}}{d X_{2}} d X_{2}

∴

Given

{\overline{B}}_{2} (X_{2})

, we can compute

{\overline{B}}_{1} (X_{2})

Then we can find

B = {\overline{B}}_{1} X_{1} + {\overline{B}}_{2} X_{2}

Example 8.2:

Given

Δ {\overline{H}}_{2}

, find

Δ {\overline{H}}_{1}

and

Δ H

Δ {\overline{H}}_{2} = a X_{1}^{2}

Compute total derivative:

\frac{d\Delta\bar{H}_{2}}{dX_{2}}=2aX_{1}\underset{\hookrightarrow=-1}{\frac{dX_{1}}{dX_{2}}}=-2aX_{1}

X_{1} + X_{2} = 1

d X_{1} + d X_{2} = 1

d X_{1} = - d X_{2}

Δ {\overline{H}}_{1} = - \int_{X_{2} = 0}^{X_{2}} \frac{X_{2}}{X_{1}} \frac{d Δ {\overline{H}}_{2}}{d X_{2}} ⅆ X_{2} = - \int_{X_{2} = 0}^{X_{2}} \frac{X_{2}}{X_{1}} (- 2 a X_{1}) ⅆ X_{2}

Δ {\overline{H}}_{1} = 2 a \int_{0}^{X_{2}} X_{2} ⅆ X_{2} = a X_{2}^{2}

Δ H = X_{1} Δ {\overline{H}}_{1} + X_{2} Δ {\overline{H}}_{2} = X_{1} (a X_{2}^{2}) + X_{2} (a X_{1}^{2}) = a X_{1} X_{2} \underset{= 1}{\underset{⏟}{(X_{1} + X_{2})}}

Δ H = a X_{1} X_{2}

14.5 Relationships between partial molal properties:

(F', G', H', S', U', their derivative, and coefficient relations)

Apply differential operator

{(\frac{\partial}{\partial n_{k}})}_{P, T, n_{j}}

to an extensive quantity:

Example: Hemholtz free energy

F^{'} = U^{'} - T S^{'}

Differentiating,

{(\frac{\partial F^{'}}{\partial n_{k}})}_{T, P, n_{j}} = {(\frac{\partial U^{'}}{\partial n_{k}})}_{T, P, n_{j}} - T {(\frac{\partial S^{'}}{\partial n_{K}})}_{T, P, n_{j}}

By definition,

{\overline{F}}_{k} = {\overline{U}}_{k} - T {\overline{S}}_{k}

See De Hoff for more examples and for coefficient an Maxwell relations.

14.6 Chemical Potential in Multicomponent Systems

Given

μ_{k} (T, P, X_{k})

, one can find

B, B^{'}, \overline{B} (T, P, X)

The thermodynamic state is specified by C+2 variables:

d U^{'} = T d S^{'} - P d V^{'} + \sum_{k = 1}^{C} μ_{k} d n_{k}

, so

μ_{k} \equiv {(\frac{\partial U^{'}}{d n_{K}})}_{S, V, n_{j}}

From Chapter 4 then,

δ W^{'} = \sum_{k = 1}^{C} μ_{k} d n_{k}

(necessary in open systems)

Examining

d H^{'}, d F^{'}

and

d G^{'}

, we find that

Given

μ_{k} (T, P) = \overline{G_{k}}

, we can express all PMP's in terms of

μ_{k} :

{\overline{S}}_{k}, {\overline{V}}_{k}, {\overline{H}}_{k}, {\overline{U}}_{k}, {\overline{F}}_{k}

{\overline{S}}_{k} = - {(\frac{\partial {\overline{G}}_{k}}{\partial T})}_{P, n_{k}} = - {(\frac{\partial μ_{k}}{\partial T})}_{P, n_{k}}

{\overline{V}}_{k}^{'} = {(\frac{\partial {\overline{G}}_{k}}{\partial P})}_{T, n_{k}} = {(\frac{\partial μ_{k}}{\partial P})}_{T, n_{k}}

{\overline{H}}_{k} = {\overline{G}}_{k} + T {\overline{S}}_{k} = μ_{k} - T {(\frac{\partial μ_{k}}{\partial T})}_{P, n_{k}} - P {(\frac{\partial μ_{k}}{\partial P})}_{T, n_{k}}

{\overline{F}}_{k} = {\overline{U}}_{k} - T {\overline{S}}_{k} = μ_{k} - P {(\frac{\partial μ_{k}}{\partial P})}_{T, n_{k}}

μ_{k}

is not measured directly

\Rightarrow

measurement of

μ_{k} (P, T)

enables PMPs to be determined. Note that

Δ {\overline{B}}_{k}

can also be determined by substituting

μ_{k} \to Δ μ_{k} = μ_{k} - μ_{k}^{0}

14.7 Activity and Activity Coefficient

We found that

μ_{k} (T, P) = {(\frac{\partial G^{'}}{\partial n_{k}})}_{P, T, μ_{j}} \equiv {\overline{G}}_{k} (T, P)

but we do not know how to measure directly.

Define

μ_{k} - μ_{k}^{0} = Δ μ_{k} \equiv R T ln a_{k}

, where

a_{k}

is the activity of component k. Further we define the activity coefficient

γ_{k}

a_{k} = γ_{k} X_{k}

, where

X_{k}

is the mole fraction.

Δ μ_{k} = R T ln (Y_{k} X_{k})

Next step: derive this for an ideal solution.

14.8 Properties of ideal solutions (e.g. ideal gas mixtures)

Imagine removing the partitions in Figure 14.3 below and allowing the gases to mix while keeping T,P constant. The process is analogous to free expansion.

image: 42_home_ken_Mydocs_MSEcore_314_figures_compart.svg

Figure 14.3: Mixture of ideal gases

Each component experiences a decrease in pressure from P to

P_{k}

. Each gas exerts, through collisions, a partial pressure on the wall of

P_{k} = X_{k} P .

The total pressure P is

P = \sum_{k = 1}^{C} P_{k} = \sum_{k = 1}^{C} X_{k} P = P \sum_{k = 1}^{C} X_{k} = P

Consider the change in chemical potential for the component,

K

which we can find by integrating

d μ_{K} :

d μ_{k} = - {\overline{S}}_{k} d T + {\overline{V}}_{k} d P = {\overline{V}}_{k} d P

since expansion is isothermal.

For an ideal gas,

V^{'} = n_{T} \frac{R T}{P} = \frac{R T}{P} = \frac{R T}{P} \sum_{k = 1}^{C} n_{k}

for which we can find

{\overline{V}}_{k} = {(\frac{\partial V^{'}}{\partial n_{k}})}_{T, P, n_{j}} = \frac{R T}{P}

Δ μ_{k} = μ_{k} - μ_{k}^{0} = \int_{P}^{P_{k}} {\overline{V}}_{k} ⅆ P = \int_{P}^{P_{k}} \frac{R T}{P} ⅆ P = R T ln \frac{P_{k}}{P} = R T ln X_{k}

Since the activity

a_{k} = X_{k}

, we conclude that the activity coefficient

γ_{k} = 1

for an ideal gas. (no interactions)

How do the partial molal quantities vary?

Δ {\overline{G}}_{k} = R T ln X_{k}

Δ {\overline{V}}_{k} = {(\frac{\partial Δ μ_{k}}{\partial P})}_{T, n_{k}} = 0

Δ {\overline{S}}_{k} = - {(\frac{\partial Δ μ_{k}}{\partial T})}_{P, n_{k}} = - R ln X_{k}

Δ H_{k} = Δ μ_{k} + T Δ {\overline{S}}_{k} = R T ln X_{k} + T (- R ln X_{k}) = 0

Δ {\overline{U}}_{k} = Δ \overline{H_{k}} - P Δ \overline{V_{k}} = 0

Δ {\overline{F}}_{k} = Δ {\overline{U}}_{k} - T Δ {\overline{S}}_{k} = R T ln X_{k}

The change in total volume, enthalpy, and internal energy is 0, as the changes in partial molal quantities is zero. However, entropy is produced, leading to decreases in the free energies

Δ G_{m i x}, Δ F_{m i x}

image: 43_home_ken_Mydocs_MSEcore_314_figures_idealsoln.svg

Figure 14.4: Properties of an ideal solution including

Δ G_{m i x}, Δ S_{m i x}, Δ H_{m i x}, Δ V_{m i x}, Δ U_{m i x}

and

Δ F_{m i x}

. Maximum temperature shown is 1400 K.

14.9 Behavior of Dilute Solutions

Add a few atoms of component 2 (solute) to a large volume of component 1 (solvent).

The solvent atoms still behave as though they are in an ideal solution, regardless of interactions.

Raoult's Law:

\underset{X_{1 \to 1}}{l i m} a_{1} = X_{1}

The solute atoms interact primarily with solvent atoms, so the average properties will be proportional to

X_{2}

for small

X_{2} .

(However, properties depend on solvent-solute combination.)

Henry's Law:

\underset{X_{2} \to 0}{l i m} a_{2} = γ_{2}^{0} X_{2} : γ_{2}^{0} (T, P)

is Henry's Law constant (in particular range), the solute activity coefficient for a dilute solution.

Consider Solute A in Solvent B

γ_{_{2}} = e^{a_{o} X_{1}^{2} / R T}

for

X_{1} \to 1

γ_{1}^{0} = e^{α_{0} / R T}

image: 44_home_ken_Mydocs_MSEcore_314_figures_pureb.svg

Figure 14.5:

Example: HW 8.4

One mole of solid

C r_{2} O_{3}

at 2500K is dissolved in a large volume of a liquid Raoultian solution (at 2300K) of

A l_{2} O_{3}

and

C r_{2} O_{3}

(20%).

Calculate the resulting

Δ H

and

Δ S

given

T_{m, C r_{2} O_{3}} = 2538 K

Δ H_{m, A l_{2} O_{3}} = 107, 500 σ / m o l - K

T_{m}

(2324K)

Δ S_{m, A l_{2} O_{3}} = Δ S_{m, C r_{2} O_{3}}

Recall that under isobaric, reversible conditions,

Δ S^{α \to P} = \frac{Δ H^{α \to β}}{T}

\frac{Δ H_{m, 1}}{T_{m, 1}} = \frac{Δ H_{m, 2}}{T_{m, 2}} \Rightarrow Δ H_{m, C r_{2} O_{3}} = Δ H_{m, A l_{2} O_{3}} = Δ H_{m, A l_{2} O_{3}} \times \frac{T_{m, C r_{2} O_{3}}}{T_{m, A l_{2} O_{3}}}

Δ H_{m, C r_{2} O_{3}} = 107, 500 \frac{J}{m o l - K} \times \frac{2538 K}{2324 K} = 117, 400 J / m o l - K

Note:

Δ H = Δ H^{S \to L} + Δ H_{m i x}

, but for ideal solution,

Δ H_{m i x} = 0

Note: if heating of

C r_{2} O_{3}

were required we read

C_{P} (T) .

Next calculate the change in entropy due to 1) melting and 2) mixing.

“Large” liquid volume

\to

no change in

X_{C r_{2} O_{3}} \to Δ {\overline{H}}_{A l_{2} O_{3}} = 0

Focus on change in 1 mole of solid

C r_{2} O_{3} .

Δ S = Δ S_{m} + Δ S_{m i x}

Δ S_{m} = \frac{Δ H_{m}}{T_{m}} = \frac{117500}{2538} = 46.26 J / K

Δ S_{m i x} = - R ln X^{F} - (- R ln X^{i})

, where

X_{C r_{2} O_{3}}^{i} = 1

(assume

γ^{0} = 1

)

Δ S_{m i x} = - R ln (0.2)

Δ S = 46.26 + 13.38 = 59.64 J / K

image: 45_home_ken_Mydocs_MSEcore_314_figures_craidiagram.svg

Figure 14.6:

C r_{2} O_{3} - A l_{2} O_{3}

Phase Diagram

14.10 Excess Properties, relative to ideal

Δ μ_{k} = R T ln (a_{k}) = R T ln (Y_{k} X_{k})

, so we can write

Δ {\overline{G}}_{k} = \underset{}{\underset{⏟}{R T ln γ_{k}}} + \underset{}{\underset{⏟}{R T ln X_{k}}} = Δ {\overline{G}}_{k}^{X S} + Δ {\overline{G}}_{k}^{i d}

γ_{k} > 1,

the excess free energy is positive.

γ_{k} > 1

, the excess free energy is negative.

Temperature and pressure derivatives of

μ (P, T)

give the remaining properties in terms of

γ_{k} .

(See table 8.5)

. \begin{matrix} Δ H_{k} = Δ {\overline{G}}_{k} - T Δ S_{k} = Δ μ_{k} - T {(\frac{\partial μ_{k}}{\partial T})}_{P, μ_{k}} = - R T^{2} {(\frac{\partial ln γ_{k}}{\partial T})}_{P, n_{k}} \\ Δ {\overline{V}}_{k} = {(\frac{\partial Δ {\overline{G}}_{n}}{\partial P})}_{T, n_{k}} = \frac{\partial}{\partial P} {[(R T ln γ_{k} + R T ln X_{R})]}_{T, n_{k}} = R T {(\frac{\partial ln γ_{k}}{\partial P})}_{T, n_{k}} \end{matrix}}

= 0 for an ideal gas.

14.11 Beyond the ideal solution: the “regular” solution

The entropy of mixing is the same as for an ideal solution
The enthalpy of mixing is not zero, but depends on composition

Partial Molar

Δ {\overline{G}}_{k} = Δ μ_{k} = Δ {\overline{H}}_{k} - T Δ {\overline{S}}_{k}

Total Molar

Δ G_{m i x} = Δ H_{m i x} - T Δ S_{m i x}

For ideal solution,

Δ H_{m i x} = 0

, For regular :

Δ H_{m i x} = Δ H_{m i x}^{X S} (X_{2,} X_{3}, ... X_{c})

For a regular solution,

Δ S_{m i x}^{r e g} = Δ S_{m i x}^{i d},

Δ S_{m i x}^{X S} = 0

Δ G_{m i x}^{X S} = Δ H_{m i x}^{X S} - T Δ S_{m i x}^{X S}

Δ {\overline{G}}_{m}^{X S} = Δ {\overline{H}}_{k} = R T ln γ_{k}

We see that

γ_{k}

can be evaluated from the heat of mixing:

γ_{k} = e x p (\frac{Δ {\overline{H}}_{k}}{R T})

(check in eq 8.102)

Let's look at the simplest binary example:

Let

Δ H_{m i x} = a_{o} X_{1} X_{2} = Δ G_{m i x}^{X S}

, where

a_{o}

is constant. This corresponds to example 8.1. The change in Gibbs Free energy.

Δ G_{m i x} = Δ G^{X S} + Δ G^{i d} = a_{o} X_{1} X_{2} + \underset{Table 8.3}{\underset{⏟}{R T X_{1} ln X_{1} + R T X_{2} ln X_{2}}}

a_{o}

determines the departure from ideal behavior arising from interactions between components.

A more realistic model (not symmetric and temperature dependent) of a binary system is

Δ H_{m i x} = X_{1} X_{2} [α_{o} (T) X_{1} + α_{1} (T) X_{2}] = Δ G_{m i x}^{X S}

Let's examine the impact of interactions on

Δ H_{m i x}, Δ S_{m i x}

, and

Δ G_{m i x}

, starting with the simpler regular solution.

image: 46_home_ken_Mydocs_MSEcore_314_figures_Idealsoln2.svg

Figure 14.7: Properties of an ideal solution

image: 47_home_ken_Mydocs_MSEcore_314_figures_regsoln.JPG

Figure 14.8: Properties of a regular solution

Δ {\overline{S}}_{k} = - R ln γ_{k} - R ln X_{k} - R T {(\frac{\partial ln γ_{k}}{\partial T})}_{P, n_{k}}

Δ {\overline{U}}_{k} = R T^{2} {(\frac{\partial ln γ_{k}}{\partial T})}_{P, n_{k}} - P R T {(\frac{\partial ln γ_{k}}{\partial P})}_{T, n_{k}}

Δ {\overline{F}}_{k} = R T ln γ_{k} + R T ln X_{k} - P R T {(\frac{\partial ln γ_{k}}{\partial P})}_{T, n_{k}}

For reference, not lecture

Gibbs Duhem Equations

X_{1} d Δ μ_{1} + X_{2} d Δ μ_{2} = 0

Δ μ_{k} = R T ln (a_{k})

X_{1} d ln γ_{1} + X_{2} d ln γ_{2} = 0

a_{k} = γ_{k} X_{k}

Δ μ = - \int_{0}^{X_{2}} \frac{X_{2}^{'}}{X_{1}} \frac{d Δ μ_{2}}{d X_{2}^{'}} ⅆ X_{2}^{'}

ln γ_{1} = - \int_{X_{1}}^{X_{2}} \frac{X_{2}^{'}}{X_{1}} \frac{d ln γ_{2}}{d X_{2}^{'}} ⅆ X_{2}^{'}

ln a_{1} = - \int_{0}^{X_{2}} \frac{X_{2}^{'}}{X_{1}} \frac{d ln a_{2}}{d X_{2}^{'}} ⅆ X_{2}^{'}

Δ {\overline{S}}_{k} = - {(\frac{\partial Δ μ_{k}}{\partial T})}_{P, n_{k}}

Δ {\overline{H}}_{k} = Δ μ_{k} + T {(\frac{\partial Δ μ_{k}}{\partial T})}_{P, n_{k}}

Δ {\overline{G}}_{k} = Δ μ_{k} = Δ {\overline{H}}_{k} - T Δ {\overline{S}}_{k}

Δ G_{m i x} = Δ H_{m i x} - T Δ S_{m i x}

For an ideal solution,

Δ H_{m i x} = 0

, for a regular solution

Δ S_{m i x}^{r e g} = Δ S_{m i x}^{i d}

Δ G_{m i x}^{X S} = Δ H_{m i x}^{X S} - T Δ S_{m i x}^{X S}

Δ S_{m i x}^{X S} = 0

The entropy of mixing for a regular solution is the same as for an ideal solution (hence

Δ S^{X S} = 0

)

The enthalpy of mixing for a regular solution deciates from that of an ideal solution (

Δ H^{i d} = 0, Δ H^{X S} \neq 0

14.11.0.1 Example: HW 8.4

One mole of solid

C r_{2} O_{3}

at 2500 K is dissolved in a large colume of a liquid Raoultian solution (2300 K) of

A l_{2} O_{3}

and

C r_{2} O_{3}

(20%).

Calculate the resulting

Δ H

and

Δ S

given

T_{m, C r_{2} O_{3}} = 2538 K

Δ H_{m, A l_{2} O_{3}} = 107, 500

J/mol-K

@ T_{m}

(= 2324 K)

Δ S_{m, A l_{2} O_{3}} = Δ S_{m, C r_{2} O_{3}}

Recall that under isobaric, reversible conditions,

Δ S^{α \to β} = \frac{Δ H^{α \to β}}{T}

\frac{Δ H_{m, 1}}{T_{m .1}} = \frac{Δ H_{m, 2}}{T_{m, 2}} \Rightarrow Δ H_{m, C r_{2} O_{3}} = Δ H_{m, A l_{2} O_{3}} \times \frac{T_{m, C r_{2} O_{3}}}{T_{m, A l_{2} O_{3}}}

Δ H_{m, C r_{2} O_{3}} = 107, 500 \frac{J}{m o l - K} \times \frac{2538 K}{2324 K} = 117, 400 \frac{J}{m o l - K}

Note: if heating of

C r_{2} O_{3}

were required, we need

C_{P} (T) .

Next calculate changes in entropy due to 1) melting and 2) mixing.

“Large” liquid volume

\to

no change in

X_{C r_{2} O_{3}} \to Δ {\overline{H}}_{A l_{2} O_{3}} = 0

Focus on change in 1 mole of solid

C r_{2} O_{3}

Δ S = Δ S_{m} + Δ S_{m i x}

Δ S = \frac{Δ H_{m}}{T_{m}} = \frac{117400}{2538} = 46.26 J / K

Δ S_{m i x} = - R ln X^{F} - (- R ln X^{i})

, where

X_{C r_{2} O_{3}}^{i} = 1

Δ S_{m i x} = - R ln (0.2)

Δ S = 46.26 + 13.38 = 59.64

J/K

14.11.1 Mixtures of Real Gases: Fugacity

Describe “real” gases in terms fo their deviation from ideal behavior, starting with molar volume

{\overline{V}}_{k}

Define

α_{k} = {\overline{V}}_{k} - \frac{R T}{P}

(note that

α_{k} = 0 \leftrightarrow i d e a l

)

The change in chemical potential with mixing is then

Δ μ_{k} = \int_{P}^{P_{k}} (α_{k} + \frac{R T}{P^{'}}) ⅆ P^{'} = \int_{P}^{P_{k}} α_{k} ⅆ P^{'} + R T ln (\frac{P_{k}}{P})

Introduce fugacity

f_{k}

Δ μ_{k} \equiv RT ln (\frac{f_{k}}{P})

Note:

a_{k} = \frac{f_{k}}{P}

Taking the exponential, we get

f_{k} = P_{k} e x p [\int_{P}^{P_{μ}} α_{k} ⅆ P]

α_{k} \to 0

f_{k} \to P_{k}

Determination of fugacity (or

a_{k}

)

\leftrightarrow

finding

μ (P, T)

Key goal of 314-316 Sequence: Predict Microstructure

image: 48_home_ken_Mydocs_MSEcore_314_figures_microstructure.JPG

Figure 14.9: Calculated and observed microstructures

image: 49_home_ken_Mydocs_MSEcore_314_figures_multicomp.JPG

Figure 14.10: Multicomponent heterogeneous (multi-phase) system

15 Multicomponent Heterogeneous Systems

Outcomes for this section:

Write a combined statement of the first and second law of thermodynamics for multiple phases.
State the conditions for equilibrium for an arbitrary number of phases and components.
State the Gibbs phase rule and apply it to the description of unary and binary phase diagrams.
Given a single component phase diagram in terms of pressure and temperature, construct alternative representations that enable determination of phase fractions in terms of volume of mole fraction.
Given a two-component phase diagram in terms of pressure, temperature, and activity, construct alternative representations that enable determination of phase fractions in terms of volume or mole fraction.
Use the lever rule to compute phase fractions from temperature versus composition diagrams.

Define conditions for equilibrium
Derive Gibbs Phase Rule
Structure of 1 and 2 component phase diagrams
The Lever Rule

Consider

P V = R T

(ideal gas)

There are two degrees of freedom: E.g. choose

P, T

(independent)

\to

V

(dependent) is determined

Equilibrium between 2 phases implies that the system is in equilibrium.

Homogeneous system:

d U^{'} = \underset{(}{T d S^{'}} - \underset{(}{P d V^{'}} + \underset{(}{\sum_{k = 1}^{C} μ_{k} d n_{k}}

image: 50_home_ken_Mydocs_MSEcore_314_figures_greenphases.svg

Figure 15.1: Multicomponent heterogeneous and homogeneous systems

Heterogeneous System:

d U_{s y s}^{'} = \sum_{α = 1}^{P} [T^{α} d S^{' α} - P^{α} d V^{'} + \sum_{k = 1}^{C} μ_{k}^{α} d n_{k}^{α}]

image: 51_home_ken_Mydocs_MSEcore_314_figures_alphabetagamma.svg

Figure 15.2: Multicomponent heterogeneous (multi-phase) system

15.1 Conditions for Equilibrium

\begin{matrix} T^{α} = T^{β} & P^{α} = P^{β} & μ^{α} = μ^{β} \end{matrix}

likewise for all pairs of phases

β / γ, γ, ... P

, where

P =

number of phases

T^{I} = T^{I I} = ... = T^{P}

P - 1

independent equations

P^{I} = P^{I I} = ... = P^{P}

P - 1

independent equations

. \begin{matrix} μ_{1}^{I} = μ_{1}^{I I} = ... = μ_{1}^{P} \\ μ_{2}^{I} = μ_{2}^{I I} = ... = μ_{2}^{P} \\ ⋮ \\ μ_{C}^{I} = μ_{C}^{I I} = ... = μ_{C}^{P} \end{matrix}} \begin{matrix} " \\ " \\ C = # components \\ " \end{matrix}

Equilibrium conditions generate

(C + 2) (P - 1) = n

equations. These are constraints on the variables

15.2 Gibbs Phase Rule

F = C - P + 2

F = m - n

is the number of degrees of freedom

For

n

equations relating

m

variables. What is

m

. \begin{matrix} T^{I}, P^{I}, X_{2}^{I}, X_{3}^{I} ... X_{C}^{I} & 2 + C - 1 = C + 1 \\ T^{I I}, P^{I I}, X_{2}^{I I}, X_{3}^{I I} ... X_{C}^{I I} & " \\ ⋮ & ⋮ \\ T^{P}, P^{P}, X_{2}^{P}, X_{3}^{P} ... X_{C}^{P} & " \end{matrix}} P sets of C+ 1 variables

∴ m = P (C + 1)

m - n = P (C + 1) - (C + 2) (P - 1) = P C + P - P C - 2 P + C + 2

m-n=C-P+ 2

Gibbs Phase Rule

16 Phase Diagrams

Outcomes for this section:

Apply a common tangent construction to define the regions of phase stability in a $G$ versus $X$ diagram.
Use a single component $G - T$ diagram to compute $Δ G_{k}^{0, α \to β}$ .
Given $G$ versus $X$ at different $T$ , construct a phase diagram in terms of $T$ and $X$ .
Describe the influence of interactions (in a simple regular solution model) on the features of a phase diagram, including phase boundaries, their curvature, and regions of two-phase coexistence.
Describe the origins and consequences of a miscibility gap.

16.1 Unary Phase Diagrams

C = 1

F = C - P + 2

In single phase regions (

P = 1

), there are two degrees of freedom (e.g. T,P)

image: 52_home_ken_Mydocs_MSEcore_314_figures_unaryphase.svg

Figure 16.1: Unary (C=1) phase diagram

P and T required to specify state in single-phase region.
For 2-phase region, P fixes and T (and vice versa)

1 degree of freedom ( $F = 1 - 2 + 2 = 1$ )
For triple point, $F = 0$

Only three phases are possible for a single component diagram.

16.2 Alternative Representations

P - V

T - X

, etc.

Not all useful variables (e.g. V,X) are thermodynamic potentials

2-phase coexistence lines

\to

areas

image: 53_home_ken_Mydocs_MSEcore_314_figures_unaryphase2.svg

Figure 16.2: Alternate representations

To describe:

Increasing T, which increases V
Mixture of phases in regions with tie lines, average molar volume.
Triple points
Changes in enthalpy and phase fraction upon heating.

16.3 Binary Phase Diagrams

C = 2

There are 5 possible phases:

α, ε, β, L, V

F = C - P + 2

For a single phase region,

f = 3 \to

Plot in P, T,

a_{2}

space. 2-phase regions are planes, 3-phase regions are lines, and 4-phase regions are points.

image: 54_home_ken_Mydocs_MSEcore_314_figures_binaryphase.svg

Figure 16.3: Binary (c=2) phase diagram

16.4 Alternative Representations: T vs. X

In Figure 16.4 below, the 2-phase coexistence lines are areas.

image: 55_home_ken_Mydocs_MSEcore_314_figures_altrep.svg

Figure 16.4: T vs X for binary phase diagram

16.5 Interpreting Phase Diagrams: Tie Lines

For plots with two degrees of freedom, a point on the diagram corresponds to a state of the system.

Which phases are present (and #) in equilibrium
The state of the phases (P,T, or other variables).
For plots with $V$ or $X,$ the relative amounts.

Example:

State P with average composition

X_{2}^{o}

at temperature T. The phase

Σ

is in equilibrium with the liquid

(T^{Σ} \neq T^{L}) .

n_{T} X_{2}^{o} = n^{Σ} X_{2}^{Σ} + n^{L} X_{2}^{L} \to X_{2}^{o} = \frac{n^{Σ}}{n^{T}} X_{2}^{Σ} + \frac{n^{L}}{n^{T}} X_{2}^{L} = f^{Σ} X_{2}^{Σ} + f^{L} X_{2}^{L}

where n= # of moles and f= fraction

In terms of

X_{2}

X_{2}^{o} = f^{Σ} X_{2}^{Σ} + (1 - f^{Σ}) X_{2}^{L} = X_{2}^{L} + f^{Σ} (X_{2}^{Σ} - X_{2}^{o})

∴ f^{Σ} = \frac{X_{2}^{o} - X_{2}^{L}}{X_{2}^{Σ} - X_{2}^{L}}

and

f^{L} = \frac{X_{2}^{o} - X_{2}^{Σ}}{X_{2}^{L} - X_{2}^{Σ}}

These fractions can be derived from the lengths of segments of a tie line.

16.6 The Lever Rule

image: 56_home_ken_Mydocs_MSEcore_314_figures_leverrule.svg

Figure 16.5: Tie lines on an X-T diagram

f^{L} = \frac{X_{2}^{o} - X_{2}^{Σ}}{X_{2}^{L} - X_{2}^{Σ}} = \frac{A P}{A B}

f^{Σ} = \frac{X_{2}^{o} - X_{2}^{L}}{X_{2}^{Σ} - X_{2}^{L}} = \frac{P B}{A B}

X_{2}^{Σ} - X_{2}^{L} = A B

X_{2}^{Σ} - X_{2}^{o} = A P

X_{2}^{o} - X_{2}^{L} = P B

X-T diagrams gives temperature, compositions, and amounts.

16.7 Applications of Phase Diagrams: Microstructure Evolution

Following an isotherm in the X-T diagram of Figure shows the following microstructures:

$T_{o} :$ homogeneous melt
$T_{1} :$ $α + L$ (nucleation)
$T_{2} :$ increase in $α$ phase
$T_{3} :$ solidification - $α + β$

image: 57_home_ken_Mydocs_MSEcore_314_figures_microstructdiag.JPG

Figure 16.6: Microstructure Evolution

16.8 Review

Δ G_{m i x} = Δ H_{m i x} - T S_{m i x}^{i d}

Δ G_{m i x} = Δ G_{m i x}^{X S} + R T (X_{1} ln X_{1} + X_{2} ln X_{2})

Δ G_{m i x}^{i d e a l} = R T (X_{1} ln X_{1} + X_{2} ln X_{2})

image: 58_home_ken_Mydocs_MSEcore_314_figures_revimg1.JPG

Figure 16.7: Gibbs free energy of mixing for ideal vs real mixtures

Δ H_{m i x} \neq 0

: interactions change Gibbs free energy of mixing

T ↑

: particle kinetic energy increases, influence of interactions decreases, behavior is more ideal.

16.9 Types of $α - L$ phase diagrams

Δ H_{m i x} = a_{o} X_{1} X_{2}

Note the curvature of the phase boundary in Figure 16.8 below - the sign follows that of

a_{o}^{2} .

image: 59_home_ken_Mydocs_MSEcore_314_figures_alphal.svg

Figure 16.8: Patterns of phase diagrams can generated by only two phases,

α

and L, with the simplest regular solution model

17 Thermodynamics of Phase Diagrams

Goal: Generate phase diagrams from

Δ G

vs. X curves

Observe: how interactions (changing potential energy) and temperature (changing kinetic energies) influence characteristics of phase diagrams.

Approach: find common tangent lines between

Δ G_{m i x}^{α}

and

Δ G_{m i x}^{L}

to determine regions of phase stability.

Needed: comparison of solid and liquid reference states

17.1 Calculation of $Δ G_{m i x}$ from pure component reference states

We can plot

Δ G_{m i x}

for a solid

(α)

or liquid (L) solution using solid or liquid reference states for components 1,2 (4 possibilities).

One cannot directly compare the following:

Need to change reference states

. \begin{matrix} Δ G_{m i x}^{α} = X_{1}^{α} ({\overline{G}}_{1}^{α} - G_{1}^{o α}) + X_{2}^{α} ({\overline{G}}_{2}^{α} - G_{2}^{o α}) \\ Δ G_{m i x}^{L} = X_{1}^{L} ({\overline{G}}_{1}^{L} - G_{1}^{o L}) + X_{2}^{α} ({\overline{G}}_{2}^{L} - G_{2}^{o L}) \end{matrix}}

Indicate choice of reference states with brackets:

Reference states the same for

α

and L phases}

. \begin{matrix} Δ G_{m i x}^{α} = X_{1}^{α} ({\overline{G}}_{1}^{α} - G_{1}^{o α}) + X_{2}^{α} ({\overline{G}}_{2}^{α} - G_{2}^{o α}) \\ Δ G_{m i x}^{L} = X_{1}^{L} ({\overline{G}}_{1}^{L} - G_{1}^{oL}) + X_{2}^{α} ({\overline{G}}_{2}^{L} - G_{2}^{oL}) \end{matrix}}

Rewrite:

Δ G_{m i x}^{α} = X_{1}^{α} ({\overline{G}}_{1}^{α} - G_{1}^{o α}) + X_{2}^{α} ({\overline{G}}_{2}^{α} - G_{2}^{o α}) - X_{2}^{α} ({\overline{G}}_{2}^{o L} - G_{2}^{o α})

Δ G_{m i x}^{α} (α, L) = X_{1}^{α} ({\overline{G}}_{1}^{α} - G_{1}^{o α}) + X_{2}^{α} + X_{2} (G_{2}^{o α} - G_{2}^{o L})

Δ G_{m i x}^{α} (α, L) = Δ G_{m i x}^{α} (α, α) + X_{2}^{α} Δ G_{2}^{o L \to α}

Similarly,

Δ G_{m i x}^{L} (α, L) = Δ G_{m i x}^{L} (L, L) + X_{1}^{L} Δ G_{2}^{o α \to L}

What do these look like?

image: 60_home_ken_Mydocs_MSEcore_314_figures_gmix.svg

Figure 17.1:

Next step: plot

Δ G^{α}, Δ G^{L}

together and find common tangent to determine regimes of phase stability.

image: 61_home_ken_Mydocs_MSEcore_314_figures_gmixes.svg

Figure 17.2:

17.2 Common Tangent Construction

The common tangent construction is a graphical represenation of two phase equilibrium for a given P,T. An example is illustrated in Figure 17.3. At this T and P, a solid of composition

X_{2}^{α}

can be in equilibrium with a liquid of composition

X_{2}^{L} (T^{α} = T^{L}, P^{α} = P^{L}, μ_{1}^{α} = μ_{1}^{L}, μ_{2}^{α} = μ_{2}^{L})

image: 62_home_ken_Mydocs_MSEcore_314_figures_commontan.svg

Figure 17.3: Common tangent construction

The intercepts reflect the conditions for chemical equilibrium.

. \begin{matrix} Δ μ_{1}^{α} = μ_{1}^{α} (X_{2}^{α}) - μ_{1}^{o α} \\ Δ μ_{1}^{L} = μ_{2}^{L} (X_{2}^{L}) - μ_{1}^{o α} \end{matrix}} μ_{1}^{α} (X_{2}^{α}) = μ_{1}^{L} (X_{2}^{L})

Chemical equilibrium of component 1 between

α, L

. \begin{matrix} Δ μ_{2}^{α} = μ_{2}^{α} (X_{2}^{α}) - μ_{2}^{o α} \\ Δ μ_{2}^{L} = μ_{2}^{L} (X_{2}^{L}) - μ_{2}^{o α} \end{matrix}} μ_{2}^{α} (X_{2}^{α}) = μ_{2}^{L} (X_{2}^{L})

Chemical equilibrium of component 2 between

α, L .

When are two-phase regions

(α + L, α + β)

stable at intermediate compositions?

image: 63_home_ken_Mydocs_MSEcore_314_figures_twophase.svg

Figure 17.4:

. \begin{matrix} X_{2} < D : α \\ X_{2} > F : β \end{matrix}} homogeneous mixtures of 1 and 2

D < X_{2} < F : α + β

has lower energy than homogeneous mixture of 1 and 2

B : Δ G

for 1 & 2 in

β

phase

A : Δ G

for 1 & 2 in

α

phase

M : Δ G

for

\frac{E F}{D F}

α

and

\frac{D E}{D F}

β

Δ G_{M} < Δ G_{A} < Δ G_{B}

Sequential transitions between multiple two-phase regions 3 solid phases, 1 liquid phase

image: 64_home_ken_Mydocs_MSEcore_314_figures_seqtrans.JPG

Figure 17.5:

How are the single and two phase regions represented on a phase diagram?

image: 65_home_ken_Mydocs_MSEcore_314_figures_singleandtwo.JPG

Figure 17.6: Representing single and two phase regions on a phase diagram

We need

Δ G (X)

for many temperature. Examine

G^{α} (T)

and

G^{P} (T) .

To generate

Δ G_{m i x}

vs.

X

curves, we need

G (T)

of pure components to establish “hanging points” (the

Δ G_{i}^{o α \to β}

)

image: 66_home_ken_Mydocs_MSEcore_314_figures_deltagvsx.svg

Figure 17.7: G(T) of pure components

Next, examine changes in

Δ G_{m i x}^{α}

and

Δ G_{m i x}^{L}

versus T to establish which phases are present.

17.3 A Monotonic Two-Phase Field

image: 67_home_ken_Mydocs_MSEcore_314_figures_monotonic.svg

Figure 17.8:

a_{o}^{α} = 1000 J / m o l

a_{o}^{L} = - 6000 J / m o l

Δ H_{m i x} = a_{o} X_{1} X_{2}

17.4 Non-monotonic Two-Phase Field

a_{o}^{α} = 6000 J / m o l

a_{o}^{L} = - 2000 J / m o l

Δ H_{m i x} = a_{o} X_{1} X_{2}

image: 68_home_ken_Mydocs_MSEcore_314_figures_nonmon.svg

Figure 17.9:

17.5 Properties of a regular solution

Recall: Regular -

Δ G_{m i x}^{i d} + Δ G_{m i x}^{X S}

image: 69_home_ken_Mydocs_MSEcore_314_figures_hmix.svg

Figure 17.10: Variation of mixing properties with composition and temperature for the simplest regular solution model. Maximum temperature is 1200 K, and

a_{o} = 12, 500 J / m o l

17.6 Misciblity Gap: Appearance Upon Cooling

Δ H_{m i x} = 13.7 X_{1} X_{2} k J / m o l

: below critical T, mixture is driven towards phase separation

a_{o}^{α} = 13, 700 J / m o l

image: 70_home_ken_Mydocs_MSEcore_314_figures_miscibility.svg

Figure 17.11: Miscibility gap

17.7 Spinodal decomposition: concave down region in $Δ G$ drives unmixing and “uphill” diffusion

image: 71_home_ken_Mydocs_MSEcore_314_figures_spinodal.JPG

Figure 17.12: Spinodal decomposition

18 Summary of 314

The summary is presented in terms of a set of detailed learning outcomes, coupled to the chapters in Dehoff. These are things you should be able to do after completing 314.

18.1 Chapters 2 and 3

State the first, second and third laws of thermodynamics.
Write a combined statement of the first and second laws in differential form.
Given sufficient information about how a process is carried out, describe whether entropy is produced or transferred, whether or not work is done on or by the system, and whether heat is absorbed or released.
Quantitatively relate differentials involving heat transfer/production, entropy transfer/production, and work.

18.2 Chapter 4

Derive differentials of state functions ( $V$ , $S$ , $U$ , $F$ , $H$ , $G$ ) in terms of $d P$ and $d T$ .
Using the Maxwell relations, relate coefficients in the differentials of state functions.
Define the coefficient of thermal expansion, compressibility, and heat capacity of a material.
Express the differential of any given state function in terms of the differentials of two others.
Define reversible, adiabatic, isotropic, isobaric, and isothermal processes.
Calculate changes in state functions by defining reversible paths (if necessary) and integrating differentials for (a) an ideal gas, and (b) materials with specified $α$ , $β$ , and $C_{P} (T)$ . (Multiple examples are given for ideal gas, solids, and liquids.)
Special emphasis (Example 4.13): calculate the change in Gibbs free energy when one mole of a substance is heated from room temperature to an arbitrary temperature at constant pressure.
Describe the origin of latent heat, and employ this concept in the calculation of changes in Gibbs free energy $G$ .

18.3 Chapter 5

Derive the condition for equilibrium between two phases.
Show that at constant temperature and pressure, the equilibrium state corresponds to that which minimizes the Gibbs free energy $G$ .
Explain why the evolution to a state of lower Gibbs free energy occurs spontaneously.

18.4 Chapter 6

Express the entropy $S$ of the system in terms of equivalent microstates in the equilibrium (most probable) macrostate.
Given the energy levels of a system of particles, calculate the partition function.
Given the partition function, calculate the Helmholtz free energy, the entropy, the internal energy, and the heat capacity.

18.5 Chapter 7

State the differential of the Gibbs free energy $G$ as a function of $S$ , $T$ , $V$ , and $P$ .
State the conditions for two phases to coexist in equilibrium.
Explain how isobaric section of the chemical potential $μ (T, P)$ as a function of temperature and pressure can be calculated from knowledge of the heat capacity and the entropy at room temperature.
Given $μ (T, P)$ for multiple phases, determine the equilibrium phase at a given temperature.
Derive the Clausius-Clapeyron relation: express the general condition for determining the region of two-phase coexistence.
Calculate the $Δ H$ given the $C_{P} (T)$ , assuming a negligible contribution from thermal expansion.
Calculate $Δ V^{α \to β}$ assuming ideal gas behavior.
Integrate $\frac{d P}{d T} = \frac{Δ S}{Δ V}$ with the assumption that $Δ S$ and $Δ V$ depend only weakly on the temperature.
Given the $P - T$ diagram, qualitatively sketch $G (T)$ for a specified region.
Given the $P - T$ diagram, specify the sign of $Δ V^{α \to β}$ .
State Trouton's rule and justify its validity qualitatively.
Sketch the $P - T$ diagram for a one-component system.

18.6 Chapter 8

Given sufficient information about the dependence of a total property $B$ or $Δ B$ versus composition, find the partial molal properties as a function of composition via calculations of derivatives $d B$ or $d Δ B$ .
Given the partial molal properties as a function of composition, calculate the total properties of the system via integration of the derivatives.
Given the differentials of state functions, write partial derivatives that define the partial molal properties.
What is $B_{k}^{0}$ ?
What is $μ_{k} - μ_{k}^{0}$ for (a) a component behaving ideally, and (b) in general?
Define the activity of a component.
Given $μ_{k} (T, P, X_{k})$ , calculate changes in the partial molal properties.
State and justify/explain Raoult's law.
State and justify/explain Henry's law.
Explain how the activity coefficient $γ$ can be used to describe the departure from ideal behavior in terms of ``excess'' quantities.
Define a ``regular'' solution and calculate the partial molal properties and total properties versus composition for binary mixtures.
Describe the driving forces for mixing and their origins in statistical mechanics.
Interpret changes in state functions with mixing in terms of ideal behavior and departures from ideality.

18.7 Chapter 9

Write a combined statement of the first and second law of thermodynamics for multiple phases.
State the conditions for equilibrium for an arbitrary number of phases and components.
State the Gibbs phase rule and apply it to the description of unary and binary phase diagrams.
Given a single component phase diagram in terms of pressure and temperature, construct alternative representations that enable determination of phase fractions in terms of volume of mole fraction.
Given a two-component phase diagram in terms of pressure, temperature, and activity, construct alternative representations that enable determination of phase fractions in terms of volume or mole fraction.
Use the lever rule to compute phase fractions from temperature versus composition diagrams.

18.8 Chapter 10

Apply a common tangent construction to define the regions of phase stability in a $G$ versus $X$ diagram.
Use a single component $G - T$ diagram to compute $Δ G_{k}^{0, α \to β}$ .
Given $G$ versus $X$ at different $T$ , construct a phase diagram in terms of $T$ and $X$ .
Describe the influence of interactions (in a simple regular solution model) on the features of a phase diagram, including phase boundaries, their curvature, and regions of two-phase coexistence.
Describe the origins and consequences of a miscibility gap.

19 314 Problems

19.1 Phases and Components

19.1.0.1

(2014) For each of the following thermodynamic systems, indicate the number of components, the number of phases, and whether the system is open or closed.

An open jar of water at room temperature (assume that the jar defines the boundaries of the system). Assume that the water molecules do not dissociate.
A sealed jar of water at room temperature.
A sealed jar of water with ice.
An open jar of water with NaCl entirely dissolved within.
If the jar is left open, in what ways might your description change?
How would your answer to (a) change if you take into account equilibrium between water, protons, and hydroxyl ions?

19.2 Intensive and Extensive Properties

19.2.0.1

(2014) Classify the following thermodynamic properties are intensive or extensive:

The mass of an iron magnet.
The mass density of an iron magnet.
The concentration of phosphorous atoms in a piece of doped silicon.
The volume of the piece of silicon.
The fraction by weight of copper in a penny.
The temperature of the penny in your pocket.
The volume of gas in a hot air balloon.

19.3 Differential Quantities and State Functions

19.3.0.1

(2014) Consider the function

z = 6 x^{2} y^{3} {cos}^{2} u

Write down the total differential of z. Identify the coefficients of the three differentials in this expression as partial derivatives.
Demonstrate that three Maxwell relations (see section 2.3) hold between the coefficients identified under (a).

19.3.0.2

(2014) Why are state functions so useful in calculating the changes in a thermodynamic system?

19.3.0.3

(2014) Derive equation 4.41 starting from 4.34 and 4.31. Note that other equations listed in table 4.5 can be derived in a similar fashion.

19.4 Entropy

19.4.0.1

(2015) Following Section 3.6, compute the change in entropy in the formation of one mole of

S i O_{2}

from Si and O at room temperature.

19.4.0.2

(2015) Consider an isolated system consisting of three compartments A, B, and C. Each compartment has the same volume V, and they are separated by partitions that have about. Initially, the valves are closed and volume A is filled with an ideal gas to a pressure

P_{0}

at 298 K. Volumes B and C are under vacuum.

Calculate the change in entropy when the valve between compartment A and B is opened.
Calculate the change in entropy when the valve between compartment B and compartment C is opened.
Without considering the calculations above, how would you know that the overall change in entropy is positive?
What would you need to do to the system to restore the initial condition?

19.5 Thermodynamic Data

19.5.0.1

(2015) This problem requires you to find sources to look up the values of important materials parameters that will be used to compute thermodynamic functions.

Find values of the coefficient of thermal expansion for a metal, a semiconductor, an insulator, and a polymer. Provide the information below in your answer.

Material Type

Specific Material

$α$

Source (include page or link info)

Elemental Metal

e.g. Gold

Semiconductor

Insulator

Polymer

What is a common material with a negative $α$ ?
How is the coefficient of compressibility related to the bulk modulus?
Which metal has the highest bulk modulus at room temperature, and what is the value?
The heat capacity is an extensive quantity. Define the related intensive quantity.
What trend do you observe in elemental solids?
What is the smallest value you can find for a solid material? (Explain your search method, and cite your sources.)

19.5.0.2

(2014) The density of silicon carbide at 298 K and 1 atm is ~3.2 g/cm³. Estimate the molar volume at 800 K and a pressure of 1000 atm. See tables 4.1 and 4.2 on page 61 of DeHoff for useful materials parameters.

19.5.0.3

(2015) The density of aluminum at 298 K and 1 atm (or “bar”) is 2.7 g/cm3. Estimate the molar volume at 1000 K and a pressure of 1000 atm. See tables 4.1 and 4.2 on page 61 of DeHoff, and Appendix B, for useful materials parameters. Hint: break the problem into two steps, each corresponding to a path.

19.5.0.4

(2015) Use the car mileage dataset provided to do the following:

Create a second order polynomial fit to determine the coefficients for the mileage dataset online. Use the systems of equations we developed during discussion to help you solve for the coefficients. Write your polynomial coefficients down in your submitted assignment.
Using your curve of best fit, determine the optimal speed for driving that maximizes your mileage.
Identify an obvious failure of your model and comment on it below.

19.5.0.5

(2015) Answer the following questions using the heat capacity dataset and the following model:

C_{p} = a + b T + c / T^{2} + d T^{2}

Use the system of equations derived in class to determine the coefficients a, b, c, d.
Give a possible Gibbs free energy function for bulk silicon using your heat capacity fit. The Gibbs free energy is related to the heat capacity through the following equation:
$C_{p} = - T {(\frac{\partial^{2} G}{\partial T^{2}})}_{P}$

19.5.0.6

(2015) Compare the change in entropy for the specific examples below of isothermal compression and isobaric heating of gases and solids.

One mole of nitrogen ( $N_{2}$ ) at 1000 K is compressed isothermally from 1 to 105 bar.
One mole of silicon at 300 K is compressed isothermally from 1 to 105 bar.
One mole of oxygen (O2) at 300 K is heated isobarically from 300 to 1200 K.
One mole of tungsten at 300 K is heated isobarically from 300 to 1200 K.

19.5.0.7

(2015) For each of the following processes carried out on one mole of a monatomic ideal gas, calculate the work done by the gas, the heat absorbed by the gas, and the changes in internal energy, enthalpy, and entropy (of the gas). The processes are carried out in the specified order.

Free expansion into the vacuum to twice the volume, starting from 300 K and 4 bar. Then,
Heating to 600 K reversibly with the volume held constant. Then,
Reversible expansion at constant temperature to twice the volume of the previous state. Then,
Reversible cooling to 300 K at constant pressure.

19.5.0.8

(2015) Consider one mole of a monatomic ideal gas that undergoes a reversible expansion one of two ways.

Under isobaric conditions, the gas absorbs 5000 J of heat in the entropy of the gas increases by 12.0 J/K. What are the initial and final temperatures of the gas?
Under isothermal conditions, 1600 J of work is performed, resulting in an entropy increase of 5.76 J/K and a doubling of the volume. At what temperature was this expansion performed?

19.5.0.9

(2015) In class we learned that the change in entropy of a material with temperature is given by:

\begin{matrix} S_{2} - S_{1} = \int_{T_{1}}^{T_{2}} \frac{C_{p} (T)}{T} ⅆ T & (19.1) \end{matrix}

In a prior homework, we fit the heat capacity to a polynomial, which we could then integrate. Now, we will numerically integrate the data points using the Trapezoid Rule discussed in class:

\begin{matrix} \int_{T_{1}}^{T_{2}} f (x) \approx (T_{2} - T_{1}) [\frac{f (T_{1} + f (T_{2}))}{2}] & (19.2) \end{matrix}

where the function

f (T)

in our case is the right hand side of Equation , is simply the right hand side of Equation 19.1. Do this by creating a “FOR” loop in MATLAB that sums up all the trapezoids in the temperature range. Email your MATLAB script to the TA by the due date.

What is the difference in entropy at 300 K and 1300 K?
Previously, we determined that the heat capacity is given by:
1. $\begin{matrix} C_{p} = 22.83 + 3.826 x 1 0^{- 3} T - \frac{3.533 x 1 0^{5}}{T^{2}} + 2.131 x 1 0^{- 8} T^{2} & (19.3) \end{matrix}$
2. Use Equation 19.1 to analytically solve for the change in entropy using Equation 19.3. Which method do you think is more accurate? Explain your reasoning.

19.6 Temperature Equilibration

19.6.0.1

(2015) 100 g of ice at 250 K is added to 100 g of water at 300 K, and the mixture is allowed to come to equilibrium in an isolated container at constant pressure. You may assume that

C_{p}

is constant for this problem (though it is not the same for water and ice) and that the melting point is 273 K.

What is the final temperature?
How much liquid is present?
How would your answer change if the initial liquid was 40% ethanol?

19.6.0.2

(2015) A square block of Al, initially at a uniform temperature of 300 K, is brought into contact with another block of aluminum, initially at a uniform temperature of 600K. Both blocks are of equal mass, and they are isolated at constant pressure while they come to equilibrium. The questions below assume equilibrium has been reached.

What do you know about the final temperatures of the Al blocks?
Will the final temperature(s) be 450 K? Justify your answer.
Find the final temperature.

19.7 Statistical Thermodynamics

19.7.0.1

(2015) DeHoff 6.3: Consider a system of two particles (A and B) that may each occupy any of the four energy levels (

ε_{1}, ε_{2}, ε_{3}, ε_{4}

How many distinct microstates are there for this system?
List each of the microstates and indicate which microstates have the same energy.
How many macrostates are there?
List the most probable macrostates.

19.7.0.2

(2015) DeHoff 6.5 Variant: Consider the system consisting of 9 identical but distinguishable particles, each of which can be in any of three states. The respective energy levels of the states are

ε_{0} = 0, ε_{1} = ε, ε_{2} = 2 ε

. The system has a temperature T.

Write the partition function for a single particle.
Calculate the average number of particles in each state.
Determine the number of configurations that have the following occupation numbers for the three states: $n_{0} = 4, n_{1} = 3, n_{2} = 2$ .
Calculate the entropy of the macrostate described by the occupation numbers above.
Calculate the internal energy.
Choose a different set of occupation numbers to give the same internal energy (e.g. (3,5,1)) and repeat your calculation of the entropy. Which macrostate is more likely?

19.7.0.3

(2015) DeHoff 6.7 variant: A System containing 500 particles and 15 energy levels is in the following macrostate: {14, 18, 27, 38, 51, 78, 67, 54, 32, 27, 23, 20, 19, 17, 15}. Estimate the change in entropyu when the system undergoes a process leading to the following changes in occupation numbers: {0, 0, -1, -1, -2, 0, 1, 0, 3, 2, -1, 1, -1, 0, -1}.

19.8 Single Component Thermodynamics

19.8.0.1

(2015) DeHoff 6.10: Compute the change in entropy when one mole of a monatomic ideal gas is compressed from an initial condition at 273K and 1 bar to 500K at 3.5 bar.

Calculate using the phenomenological thermodynamics of Chapter 4.
Calculate using the results of statistical thermodynamics. Hint: first calculate the initial and final volumes.

19.8.0.2

(2015) DeHoff 7.5: Sketch

G (T)

for an element that the pressure corresponding to the triple point. Repeat the sketch for a pressure slightly above and slightly below the triple point.

image: 72_home_ken_Mydocs_MSEcore_314_figures_triplepoint.svg

19.8.0.3

(2015) DeHoff 7.6 See Lecture 17, last page.

19.8.0.4

(2015) DeHoff 7.7 variant: At what pressure will ice melt at -2°C?

19.8.0.5

(2015) DeHoff 7.8: At 1 atm pressure and below 1155 K, the

ϵ

form of titanium is stable; above 1155 K, the

β

form is the stable phase (

ϵ

becomes metastable). Given the following data:

$Δ S^{ϵ \to β} = 3.43 J / m o l \cdot K$ (This is the difference in molar entropy 3 between the phases).
The change in molar entropy upon melting is $9.02 J / m o l \cdot K$ .
T m β =1940 K.
1. Sketch $G^{ϵ}$ , $G^{β}$ and $G^{ℓ}$ in the temperature range of interest.
2. What is $T_{m}^{ϵ}$ ?
3. There is a database of the Gibbs free energy of 78 pure elements as a function of temperature. The database can be found here: http://www.crct.polymtl.ca/sgte/unary50.tdb
  1. Find the $ϵ$ phase of titanium (labeled as GHSERTI), the $β$ phase (labeled as GBCCTI), and the liquid phase (labeled as GLIQTI) and repeat a and b using the empirical formulas. Compare your answers and comment on the accuracy of your assumptions.
  NOTE: The formula is written so that a program called Thermocalc can read them. Each free energy curve is a piecewise formula. The “;” separates the parts of the function over different temperature ranges. In addition, a “**” is the same as an exponent or “^”.

19.9 Mulitcomponent Thermodynamics

19.9.0.1

(2015) DeHoff 8.1: Titanium metal is capable of dissolving up to 30 atomic percent oxygen. Consider a solid solution in the system Ti–O containing an atom fraction,

X_{0} = 0.12

. The molar volume of this alloy is 10.68 cc/mol. Calculate the following:

The weight percent of O in the solution.
The molar concentration (mol/cc) of O in the solution.
The mass concentration (gm/cc) of O in the solution.
Use these calculations to deduce general expressions for weight percent, molar, and mass concentrations of a component in a binary solution in terms of the atom fraction, $X_{2}$ , the molar volume, $V$ , and the molecular weights, $M W_{1}$ and $M W_{2}$ , of the elements involved.

19.9.0.2

(2015) DeHoff 8.4: Use the partial molal volumes computed in Problem 8.3 (worked out in class) to demonstrate that the Gibbs – Duhem equation holds for these properties in this system.

19.9.0.3

(2015) DeHoff 8.6: For an ideal solution it is known that, for component 2,

Δ G_{2} = R T ln X_{2}

. Use the Gibbs – Duhem integration to derive corresponding relation for component 1.

19.9.0.4

(2015) One mole of solid

C r_{2} O_{3}

at 2500 K is dissolved in a large volume of a liquid Raoultian solution (also at 2500 K) of

A l_{2} O_{3}

and

C r_{2} O_{3}

with

X_{C r_{2} O_{3}}

= 0.2. Calculate the resulting changes in the total enthalpy and entropy given the following:

T_{m, C r_{2} O_{3}} = 2538 K

;

Δ H_{m, A l_{2} O_{3}} = 107, 500 J / m o l a t T_{m, A l_{2} O_{3}} = 2324 K

;

Δ S_{m, A l_{2} O_{3}} = Δ S_{m, C r_{2} O_{3}}

19.10 Computational Exercises

19.10.0.1

(2015) For this problem, you will be using MATLAB’s symbolic solver (fzero) and function handles to find the zero of an equation. On last week’s quiz we found that 89.1 grams of ice were necessary to cool a 1 kg block of Pb down to 300 K from 600 K. We will be plotting the change in temperature for both the Pb and ice. You will need the following parameters:

\begin{matrix} C_{p}^{P b} = 0.1169 + 4.2 x 1 0^{- 5} T \frac{k g}{k g \cdot K} \\ C_{p}^{H_{2} O} = 4.2 \frac{k J}{k g \cdot K} \\ Δ H_{f u s}^{H_{2} O} = 344 \frac{k J}{k g} \\ \frac{d H}{d t} = a Δ T \end{matrix}

Here

a

is a coefficient that controls the heat transfer in conduction, which we will assume to be

3.33 x 1 0^{- 3} k J / K \cdot s,

and

Δ T

is the temperature difference between the two materials.

19.10.0.2

Use the equations derived in class to plot the change in temperature for H2O and Pb. Assume dt=1 s and calculate the first 200 time steps. How do you know when the system is at equilibrium?

Create a plot that shows the amount of water in the system as a function of time. At what time is all the ice gone?
Create a plot that shows the total heat transfer occurring between the Pb and H2O. How can you tell when equilibrium is reached from this plot?

19.10.0.3

(2015) We will be putting together a program to help calculate phase diagrams of all sorts piece by piece. The first step is to create a MATLAB script that solves a system of two equations. The system is below:

\begin{matrix} G_{s} - X_{s} \frac{d G_{s}}{d X_{s}} = G_{ℓ} - X_{ℓ} \frac{d G_{ℓ}}{d X_{ℓ}} & (19.4) \end{matrix}

\begin{matrix} \frac{d G_{s}}{d X_{s}} = \frac{d G_{ℓ}}{d X_{ℓ}} & (19.5) \end{matrix}

where

G_{s}

and

G_{ℓ}

are given by the following expressions:

\begin{matrix} G_{s} (X_{s}) = Ω_{s} X_{s} (1 - X_{s}) + \\ R T [X_{s} ln X_{s} + (1 - X_{s}) ln (1 - X_{s}) + 200 X_{s} - 400 (1 - X_{s})] . \end{matrix}

G_{ℓ} (X_{ℓ}) = Ω_{ℓ} X_{ℓ} (1 - X_{ℓ}) + R T [X_{ℓ} ln X_{ℓ} + (1 - X_{ℓ}) ln (1 - X_{ℓ})] .

Here

G_{s}

is the Gibbs energy of the solid phase,

G_{ℓ}

the Gibbs free energy of the liquid phase,

R

the gas constant (8.314 J/K),

T

the absolute temperature,

X_{s}

and

X_{ℓ}

are the compositions of the solid and liquid phase respectively, and

Ω_{s}

Ω_{ℓ}

are parameters to be defined later. We can rewrite Eqs. 19.4 and 19.5 as follows:

\begin{matrix} G_{s} - X_{s} \frac{d G_{s}}{d X_{s}} - G_{ℓ} + X_{ℓ} \frac{d G_{ℓ}}{d X_{ℓ}} = 0 & (19.6) \end{matrix}

\begin{matrix} \frac{d G_{s}}{d X_{s}} - \frac{d G_{ℓ}}{d X_{ℓ}} = 0 & (19.7) \end{matrix}

Create a MATLAB function that takes

X_{s}

X_{ℓ}

T

Ω_{s}

and

Ω_{ℓ}

as inputs and then create a script that uses the MATLAB command fsolve to calculate

X_{s}

and

X_{ℓ}

for

T

=700K,

Ω_{ℓ} = 1500 c a l / m o l

and

Ω_{s} = 3000 c a l / m o l

19.10.0.4

(2015) Now that we are able to solve for the composition of the solid and liquid at one point, we will improve our script to calculate it over a range of temperatures. Start with an initial guess for both the solid and liquid near zero and a temperature of 900 K. Determine the composition of the liquid and solid down to 1 K for each temperature using a for loop. Make sure to update your guess with the correct answer for the previous temperature to help your program converge. Repeat again starting from 600 down to 1 K, this time starting with an initial guess near 1, and plot your results. Use the following parameters to make the Gibbs energy more physical:

T_{m}^{α} = 900 K

T_{m}^{β} = 600 K

Δ H_{f}^{α} = 2000 \frac{c a l}{m o l}

Δ H_{f}^{β} = 1300 \frac{c a l}{m o l}

The liquid and solid free energies are given by the following expressions. (Note that the Gibbs energy for the solid phase has changed slightly and should be adjusted in your code. In these units

R = 1.987 c a l / m o l \cdot K

\begin{matrix} G_{s} (X_{s}) = Ω_{s} X_{s} (1 - X_{s}) + R T + \\ [X_{s} ln X_{s} + (1 - X_{s}) ln (1 - X_{s}) + X_{s} Δ G_{β}^{ℓ \to s} + (1 - X_{s}) Δ G_{α}^{ℓ \to s}] . \end{matrix}

G_{ℓ} (X_{ℓ}) = Ω_{ℓ} X_{ℓ} (1 - X_{ℓ}) + R T [X_{ℓ} ln X_{ℓ} + (1 - X_{ℓ}) ln (1 - X_{ℓ})] .

As a reminder, the free energy change for the melting transition can be written in terms of the enthalpic and entropic contributions to the free energy:

Δ G^{s \to ℓ} = Δ H^{s \to ℓ} - T Δ S^{s \to ℓ}

19.10.0.5

(2015) Our phase diagram calculation is almost complete! We only have to find the equilibrium between the two solid phases left. To do that, we simply take the derivative of the Gibbs free energy of the solid phase and set it equal to zero. The equation becomes:

R T ln (\frac{X_{s}}{1 - X_{s}}) - Ω_{s} (2 X_{s} - 1)

Again, assume that

Ω_{s}

= 3000 cal/mol. This is easily done by creating a for loop that solves for the temperature at each composition between .01 and .99. Plot your results on the same figure from the previous homework and voila, your first phase diagram!

Now with your working code, replot the diagrams for the following interaction coefficients. You will have to change the range of temperatures for one of the sets below. You can figure out which one it is, if you think of the physical significance of the parameters.

$Ω_{s} = 3000 c a l / m o l : Ω_{ℓ} = 0$
$Ω_{s} = 0 : Ω_{ℓ} = 3000 c a l / m o l$
$Ω_{s} = 0; Ω_{ℓ} = 0$
$Ω_{s} = 3000 c a l / m o l : Ω_{ℓ} = 3000 c a l / m o l$
For each phase diagram, plot your results and describe how the changing interaction parameters changed the shape of the plot.

References

1"Conjugate Variables (Thermodynamics)", Wikipedia, the free encyclopedia (2015).

2"Thermodynamic Square", Wikipedia, the free encyclopedia (2016).

3DeHoff, Robert T, Thermodynamics in Materials Science (Boca Raton: CRC/Taylor & Francis, 2006).

Index

Closed system: 1
dependent variable: 1
equation of state: 1
Extensive properties: 1
First law of thermodynamics: 1
gas constant: 1
Heat Capacity: 1
Heat flow: 1
Heterogeneous system: 1
Homogeneous system: 1
Ideal gas: 1
- thermal expansion coefficient: 1
independent variable: 1
Intensive properties: 1
Internal energy: 1
Irreversible processes: 1
Isobaric: 1
Isolated system: 1
Isothermal: 1
Isothermal Compressibility: 1
Macrostate: 1
Maxwell relationships: 1
Microstate: 1
Multicomponent system: 1
Non-reacting system: 1
Open system: 1
Process variables: 1
Reacting system: 1
Reversible mechanical work: 1
Reversible processes : 1
second law of thermodynamics: 1
State Variables: 1
Temperature
- as a state function: 1
Thermite reaction: 1
Thermodynamic laws
- first law: 1
- second law: 1
- third law: 1
Third law of thermodynamics: 1
Unary system: 1

Nomenclature

$C_P$: Heat capacity at constant pressure
$C_V$: Heat capacity at constant volume
$F$: Helmholtz free energy
$G$: Gibbs free energy
$H$: Enthalpy
$P$: Pressure
$Q$: Heat
$R$: Ideal gas constant, 8.314 $J\, K^{-1}\, mol^{-1}$
$S$: Entropy
$T$: Temperature
$U$: Internal energy
$V$: Volume
$W$: Work
$\alpha$: Coefficient of thermal expansion
$\beta$: Coefficient of compressibility
$\mu$: Chemical potential
$n$: Number of moles
$n_k$: Moles of component k

Material Type	Specific Material	$α$	Source (include page or link info)
Elemental Metal	e.g. Gold
Semiconductor
Insulator
Polymer

314: Thermodynamics of Materials

Table of Contents

Catalog Description

Course Outcomes

1 314: Thermodynamics of Materials

2 Introduction

3 Big Ideas of Thermodynamics

3.1 Classification of Systems

3.2 Thermodynamic State Variables

3.3 Process Variables

3.3.1 Work Done by an External Force

3.3.2 Work Done by an Applied Pressure

3.4 Extensive and Intensive Properties

4 The Laws of Thermodynamics

Outcomes for this section:

4.1 First Law of Thermodynamics

4.2 Second Law of Thermodynamics

4.2.1 Reversible and Irreversible Processes

4.2.2 Entropy and Heat

4.3 Third Law of Thermodynamics

4.4 Differential Quantities

5 Thermodynamic Variables and Relations

Outcomes for this section:

5.1 Enthalpy

5.2 Helmholtz Free Energy

5.3 Gibbs Free Energy

5.4 Other Material Properties

5.4.1 Volume thermal expansion coefficient

5.4.2 Isothermal Compressibility

5.4.3 Heat Capacity

5.5 Coefficient Relations

5.5.1 Internal Energy

5.5.2 Enthalpy

5.5.3 Helmholtz Free Energy

5.5.4 Gibbs Free Energy

5.6 Equation of State Relationships

5.6.1 Expression for dS

5.6.2 Expression for dV

5.6.3 Relationship between C P and C V

6 The Ideal Gas

6.1 Thermal Expansion Coefficient of an Ideal Gas

6.2 Compressibility of an Ideal Gas

6.3 Internal Energy of Ideal Gas

6.4 Specific Heat of Ideal Gas

Example:

Solution:

6.5 Some Examples of Ideal Gas Behavior

6.5.1 Free expansion of an ideal gas

6.5.2 Isothermal Compression of an Ideal Gas

6.5.3 Reversibility requires work/heat

6.5.4 Some useful relations for heat flow

7 Solids and Liquids

8 Conditions for Equilibrium

Outcomes for this section:

8.1 Finding equilibrium conditions

8.2 Energy Minima

8.2.0.1 Derive conditions for equilibrium again

8.2.0.2 Example for two component system

8.3 Maxwell Relations

8.3.0.1 Useful relations between S,T,P,V for an ideal monatomic gas

9 From Microstates to Entropy

Outcomes for this section:

9.1 Microstates and Macrostates

9.1.0.1 How many microstates correspond to a given macrostate?

9.1.1 Postulate of Equal Likelihood

9.1.2 The Boltzmann Hypothesis (to be derived)

9.2 Conditions for equilibrium

10 Noninteracting (Ideal) Gas

10.1 Ideal gas Law

11 Diatomic Gases

12 The Einstein Model of a Crystal

12.1 Thermodynamic Properties of a Crystal

13 Unary Heterogeneous Systems

Outcomes for this section:

13.1 Phase Diagrams

13.2 Chemical Potential Surfaces

13.3 μ ( T,P ) Surfaces

13.4 Clasius-Clapeyron Eq.

13.4.1 Step 1: Find Δ H( T,P )

13.4.2 Step 2: Find Δ V α → β ( T,P ) ≡ V β ( P,T ) - V α ( P,T )

5.6.1 Expression for $d S$

5.6.2 Expression for $d V$

5.6.3 Relationship between $C_{P}$ and $C_{V}$

13.3 $μ (T, P)$ Surfaces

13.4.1 Step 1: Find $Δ H (T, P)$

13.4.2 Step 2: Find $Δ V^{α \to β} (T, P) \equiv V^{β} (P, T) - V^{α} (P, T)$

16.9 Types of $α - L$ phase diagrams

17.1 Calculation of $Δ G_{m i x}$ from pure component reference states

17.7 Spinodal decomposition: concave down region in $Δ G$ drives unmixing and “uphill” diffusion