Theory of Solution Thermodynamics
-
Upload
awais-javaid -
Category
Documents
-
view
171 -
download
18
description
Transcript of Theory of Solution Thermodynamics
188
Chapter 3: Solution Thermodynamics: Theory
3.0 The Notations for Solution Thermodynamics
M = the properties of the solution
(h, s, v)
iM = partial properties (e.g., ih , is )
of species i in the solution
iM = pure-species properties
(e.g., ig , is )
189
3.1 Fundamental Property Relations
We can re-write the following
relationship (Eq. 2.13)
dg vdP sdT= − (2.13)
for a system with a total number of
moles of n, as follows
( ) ( ) ( )d ng nv dP ns dT= − (3.1)
Since ‘ng’ is f(P, T) (do you know
WHY?), we obtain the following
mathematical implication
( ) ( ) ( ), ,T n P n
ng ngd ng dP dT
P T∂ ∂⎛ ⎞ ⎛ ⎞
= +⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠ (3.2)
190
By comparing Eq. 3.1 with Eq. 3.2,
we obtain the following relationships
( ),T n
ngnv
P∂⎛ ⎞
=⎜ ⎟∂⎝ ⎠ (3.3)
and ( ),P n
ngns
T∂⎛ ⎞
= −⎜ ⎟∂⎝ ⎠ (3.4)
where
n = total # of moles or # of moles
of all chemical species in the
solution
= 1 2 3 ... nn n n n+ + + +
(for n species)
Accordingly, ( )= 1 2 3f , , , , , ....ng T P n n n
191
Thus, we can re-write Eq. 3.2 as
follows
( ) ( ) ( )
( ), ,
1 , , j
T n P n
n
ii i P T n
ng ngd ng dP dT
P T
ngdn
n=
∂ ∂⎛ ⎞ ⎛ ⎞= +⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠
∂⎛ ⎞+ ⎜ ⎟∂⎝ ⎠∑
(3.5)
where jn is all species EXCEPT species i
The term ( ), , ji P T n
ngn
∂⎛ ⎞⎜ ⎟∂⎝ ⎠
is defined as
“CHEMICAL POTENTIAL, μi”
( ), , j
ii P T n
ngn
μ∂⎛ ⎞
= ⎜ ⎟∂⎝ ⎠ (3.6)
192
Combining Eqs. 3.2-3.6 together yields
( ) ( ) ( )1
n
i ii
d ng nv dP ns dT dnμ=
= − +∑ (3.7)
In the case that n = 1 i in x= , Eq. 3.7
can be re-written as follows
1
n
i ii
dg vdP sdT dxμ=
= − +∑ (3.8)
From Eq. 3.8, it implies that
( )= 1 2 3f , , , , , ....g T P x x x
Accordingly, it can be implied
mathematically that
,T x
g vP∂⎛ ⎞ =⎜ ⎟∂⎝ ⎠
(3.9)
and ,P x
g sT
∂⎛ ⎞ = −⎜ ⎟∂⎝ ⎠ (3.10)
193
This confirms that Gibbs free
energy still serves as a generating
function for other thermodynamic
properties, even in the system where
compositions of all species vary with
time
194
3.2 The Chemical Potential & Phase Equilibria
Consider a closed system where
2 phases co-exist and are in equilibrium
with each other
We can write Eq. 3.7 for each phase
(phases &α β ), as follows
( ) ( ) ( )1
n
i ii
d ng nv dP ns dT dnα α α α αμ=
= − +∑ (3.11)
( ) ( ) ( )1
n
i ii
d ng nv dP ns dT dnβ β β β βμ=
= − +∑ (3.12)
195
A total property of the system are
obtained when the property of each
phase is combined together, as
shown in the following equation
( ) ( )nM nM nMα β= + (3.13)
where M = any system property
Hence, by combining Eq. 3.11 with
Eq. 3.12, we obtain
( ) ( ) ( )1 1
n n
i i i ii i
d ng nv dP ns dT dn dnα α β βμ μ= =
= − + +∑ ∑
(3.14) From Eq. 3.1, we knew that
( ) ( ) ( )d ng nv dP ns dT= − (3.1)
196
Thus, Eq. 3.14 becomes
( ) ( )1 1
n n
i i i ii i
d ng d ng dn dnα α β βμ μ= =
= + +∑ ∑
1 1
0n n
i i i ii i
dn dnα α β βμ μ= =
+ =∑ ∑ (3.15)
Since this is a closed system, a
decrease in the number of moles of
Phase α will result in an increase in
the same number of moles of Phase
β , or vice versa, or it means that
i idn dnα β= − (3.16)
Combining Eq. 3.15 with Eq. 3.16
yields
197
( )α α β αμ μ= =
+ − =∑ ∑1 1
0n n
i i i ii i
dn dn
( )α β αμ μ=
− =∑1
0n
i i ii
dn
and, eventually
i iα βμ μ= (3.17)
This principle can also be
extended to any phases, as follows
....i i i iα β χ πμ μ μ μ= = = =
“Multiple phases at the same T &
P are in equilibrium with one
another when the chemical
potential of each species is the
same for all phases”
198
3.3 Partial Properties
We can extend the principle of
chemical potential (Eq. 3.6) to any other
thermodynamic properties, as follows
( ), , j
ii P T n
nMM
n∂⎛ ⎞
= ⎜ ⎟∂⎝ ⎠ (3.18)
where M = any system property
(e.g., h, s)
This is called “PARTIAL PROPERTY” or
“RESPONSE FUNCTION”, which represents
the change in the total property, nM, due
to the addition of a small (differential)
amount of (moles of) species i, at constant
T & P, to the solution
199
Combining Eqs. 3.6 & 3.18 together
results in
( ), , j
i ii P T n
ngg
nμ
∂⎛ ⎞= = ⎜ ⎟∂⎝ ⎠
(3.19)
This implies that the ‘chemical
potential’ is, in fact, ‘partial Gibbs
free energy’
200
3.3.1 Properties & Partial Properties
We can extend Eq. 3.5 to any other
thermodynamic properties (M) as
follows
( ) ( ) ( )
( ), ,
1 , , j
T n P n
n
ii i P T n
nM nMd nM dP dT
P T
nMdn
n=
∂ ∂⎛ ⎞ ⎛ ⎞= +⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠
∂⎛ ⎞+ ⎜ ⎟∂⎝ ⎠∑
(3.20)
and when combining Eq. 3.20 with Eq.
3.18, we obtain
( ) ( ) ( )
, ,
1
T n P n
n
i ii
nM nMd nM dP dT
P T
Mdn=
∂ ∂⎛ ⎞ ⎛ ⎞= +⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠
+∑
(3.21)
201
Since n = total # of moles of all species
in the solution, it must be constant; thus,
( )
, ,
1
T n P n
n
i ii
M Md nM n dP n dTP T
Mdn=
∂ ∂⎛ ⎞ ⎛ ⎞= +⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠
+∑ (3.22)
For a special case, when n = 1, we
obtain the following relationships
, ,T n T x
M MP P
∂ ∂⎛ ⎞ ⎛ ⎞=⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠
and , ,P n P x
M MT T
∂ ∂⎛ ⎞ ⎛ ⎞=⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠
Thus, Eq. 3.22 can be re-written as
follows
( )
, ,
1
T x P x
n
i ii
M Md nM n dP n dTP T
Mdn=
∂ ∂⎛ ⎞ ⎛ ⎞= +⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠
+∑ (3.23)
202
Consider the term 1
n
i ii
Mdn=∑ in Eq. 3.23
Since ii
nxn
= i in x n=
Thus,
( )i i i idn d x n x dn ndx= = +
Accordingly,
( )1 1
n n
i i i i ii i
Mdn M x dn ndx= =
= +∑ ∑ (3.24)
Consider the term ( )d nM in Eq. 3.23
( )d nM ndM Mdn= + (3.25)
Combining Eqs. 3.23-3.25 together
yields
203
( )
, ,
1
T x P x
n
i i ii
M MndM Mdn n dP n dTP T
M x dn ndx=
∂ ∂⎛ ⎞ ⎛ ⎞+ = +⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠
+ +∑
Rearranging the above equation
yields
, ,
0
i iT x P x
i i
M MdM dP dT Mdx nP T
M x M dn
⎡ ⎤∂ ∂⎛ ⎞ ⎛ ⎞− − −⎜ ⎟ ⎜ ⎟⎢ ⎥∂ ∂⎝ ⎠ ⎝ ⎠⎣ ⎦+ − =⎡ ⎤⎣ ⎦
∑
∑
(3.26) Eq. 3.26 will be true only if
, ,
0i iT x P x
M MdM dP dT MdxP T
⎡ ⎤∂ ∂⎛ ⎞ ⎛ ⎞− − − =⎜ ⎟ ⎜ ⎟⎢ ⎥∂ ∂⎝ ⎠ ⎝ ⎠⎣ ⎦∑
and
0i iM x M− =⎡ ⎤⎣ ⎦∑
204
Hence,
, ,
i iT x P x
M MdM dP dT MdxP T
∂ ∂⎛ ⎞ ⎛ ⎞= + +⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠∑ (3.27)
i iM x M= ∑ (3.28)
Note that Eq. 3.27 is a special case of
Eq. 3.23 when 1n = and, thus, i in x=
Multiplying Eq. 3.28 with n yields
( )i inM x n M= ∑
i inM n M= ∑ (3.29)
Eq. 3.29 is called “summability relations”
Differentiating Eq. 3.28 gives
i i i idM x dM Mdx= +∑ ∑ (3.30)
205
Combining Eq. 3.27 with Eq. 3.30 yields
, ,
i i i i
i iT x P x
x dM Mdx
M MdP dT MdxP T
+ =
∂ ∂⎛ ⎞ ⎛ ⎞+ +⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠
∑ ∑
∑
Rearranging the above equation gives
, ,
0i iT x P x
M MdP dT x dMP T
∂ ∂⎛ ⎞ ⎛ ⎞+ − =⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠∑
(3.31)
Note that Eq. 3.31 is called a Gibbs/
Duhem equation In the case where T & P are constant, a
Gibbs/Duhem equation (Eq. 3.31) becomes
0i ix dM =∑ (3.32)
206
3.3.2 Partial Properties in Binary Solutions
Consider a solution with 2 components
(in other words, a binary solution) Writing Eq. 3.28,
i iM x M= ∑ (3.28)
for a binary solution yields
1 1 2 2M x M x M= + (3.33)
Differentiating Eq. 3.33 results in
1 1 1 1 2 2 2 2dM x dM Mdx x dM M dx= + + +
(3.34)
207
Writing the Gibbs/Duhem equation
for a system where T & P are constant
results in
0i ix dM =∑ (3.32)
Eq. 3.32 can be written for a binary
solution, as follows
1 1 2 2 0x dM x dM+ = (3.35)
Combining Eq. 3.34 with Eq. 3.35
yields
( )1 1 2 2 1 1 2 2dM Mdx M dx x dM x dM= + + +
1 1 2 2dM Mdx M dx= + (3.36)
0
208
Since, for a binary solution, 1 2 1x x+ =
1 21x x= − ; hence, 1 2dx dx= − or 2 1dx dx= −
Eq. 3.36 can then be re-written as
follows:
( )
( )
1 1 2 1
1 1 2 1
1 2 1
dM Mdx M dxMdx M dxM M dx
= + −
= −
= −
1 21
dM M Mdx
= −
Rearranging the above equation
results in
1 21
dMM Mdx
= + (3.37)
209
Rearranging Eq. 3.33 gives
2 2 1 1x M M x M= −
12 1
2 2
xMM Mx x
= − (3.38)
Substituting Eq. 3.38 into Eq. 3.37 and
rearranging the resulting equation yield
1
1 12 2 1
11 1
2 2 1
xM dMM Mx x dxx M dMM Mx x dx
⎛ ⎞= − +⎜ ⎟⎝ ⎠
+ = +
2 1 1 1
2 2 1
x M x M M dMx x dx+
= + (3.39)
210
Multiplying Eq. 3.39 with x2 yields
2 1 1 1 21
dMx M x M M xdx
+ = +
( )2 1 1 21
dMx x M M xdx
+ = + (3.40)
Since 1 2 1x x+ = (for a binary system),
Eq. 3.40 can be written as follows:
1 21
dMM M xdx
= + (3.41)
By performing the same derivation
for 2M , we obtain the following equation
2 11
dMM M xdx
= − (3.42)
211
Eqs. 3.41 & 3.42 illustrate that any
partial property ( iM) can be calculated
from the property of the solution (M),
when the composition of each species
is known, which can be illustrated
graphically as follows
Let’s consider a plot between M
(M can be either h, s, or v, or etc. –
any system property) and x1 (Figure
3.1)
212
Figure 3.1: A Plot between M (any thermodynamic property) and x1
The slope of the line I1–I2 can be
calculated as follows
2 2
1 1 10M I M IdM
dx x x− −
= =−
(3.43)
and 1 21 2
1 1 0I IdM I I
dx−
= = −−
(3.44)
M
x1
I2
I1
213
Rearranging Eq. 3.43 gives
2 11
dMI M xdx
= − (3.45)
and rearranging Eq. 3.44 yields
1 21
dMI Idx
= + (3.46)
Combining Eq. 3.46 with Eq. 3.45
and rearranging result in
( )
1 11 1
11
1
dM dMI M xdx dx
dMx Mdx
⎛ ⎞= + −⎜ ⎟
⎝ ⎠
= − +
but 1 2 1x x+ = 2 11x x= −
214
Hence,
1 21
dMI M xdx
= + (3.47)
Comparing Eq. 3.47 with Eq. 3.41
and Eq. 3.45 with Eq. 3.42 yields
1 1I M= and 2 2I M=
215
Let’s consider the value of 1
dMdx
when
x1 0 (or it is called “infinite dilution of
species 1”) from Figure 3.2
Figure 3.2: A Plot between M (any thermodynamic property) and x1 when x1 0
x1
M
M2
M1
1M∞
216
Comparing Figure 3.2 with Figure
3.1 gives
1 1 1I M M∞= = and 2 2 2I M M= =
This indicates that when x1 0 (i.e.
pure x2), 2 2M M=
Let’s consider the value of 1
dMdx
when
x1 1 or x2 0 (i.e. infinite dilution of
species 2), in Figure 3.3
217
Figure 3.3: A Plot between M (any thermodynamic property) and x1 when x1 1 (or x2 0)
Comparing Figure 3.3 with Figure 3.1
yields
1 1 1I M M= = and 2 2 2I M M∞= =
meaning that when x1 1 (i.e. pure
species 1): 1 1M M=
x1
M
M2
M1 2M∞
218
Example The enthalpy of a binary
liquid system of species 1 & 2 at
constant T & P is presented by the
following equation
( )1 2 1 2 1 2400 600 40 20h x x x x x x= + + +
(3.48)
Determine the values of 1h , 2h , 1h∞ , &
2h∞
219
Rearranging Eq. 3.48 to be a
function of x1 only (note that, for a
binary system, 2 11x x= − ) gives
31 1600 180 20h x x= − − (3.49)
Differentiating Eq. 3.49 with respect
to x1 yields
21
1
180 60dh xdx
= − − (3.50)
Writing Eqs. 3.41 & 3.42
1 21
dMM M xdx
= + (3.41)
2 11
dMM M xdx
= − (3.42)
for this case yields
220
( )1 11
1 dhh h xdx
= + − (3.51)
2 11
dhh h xdx
= − (3.52)
Combining Eqs. 3.49 & 3.50 with
Eqs. 3.51 & 3.52 and rearranging give
( )( )
31 1 1
21 1
600 180 20
1 180 60
h x x
x x
⎡ ⎤= − −⎣ ⎦+ − − −
2 31 1 1420 60 40h x x= − + (3.53)
32 1600 40h x= + (3.54)
221
From Figures 3.2 & 3.3, we knew
that, when x1 0:
2 2M M= and 1 1M M∞ = and when x1 1:
1 1M M= and 2 2M M∞ =
Hence, by substituting corresponding
numerical values into Eqs. 3.53 & 3.54, we
obtain:
( ) ( ) ( )2 31 1 1 1 420 60 1 40 1 400h h x= = = − + =
( ) ( )32 2 1 0 600 40 0 600h h x= = = + =
( ) ( ) ( )2 31 1 1 0 420 60 0 40 0 420h h x∞ = = = − + =
( )32 2 1( 1) 600 40 1 640h h x∞ = = = + =
222
The values of 1h , 2h , 1h∞ , and 2h∞ can
be shown graphically as follows
0
100
200
300
400
500
600
700
0 0.2 0.4 0.6 0.8 1
x 1
h
h2
h1
2h∞
1h∞
223
3.3.3 Relations among Partial Properties
Combining Eq. 3.7
( ) ( ) ( ) i id ng nv dP ns dT dnμ= − +∑ (3.7)
with Eq. 3.19
( ), , j
i ii P T n
ngg
nμ
∂⎛ ⎞= = ⎜ ⎟∂⎝ ⎠
(3.19)
results in
( ) ( ) ( ) i id ng nv dP ns dT g dn= − +∑ (3.55)
From an “exact differential expression”,
we obtain the following relationships
224
( ) ( ), ,P n T n
nv nsT P
∂ ∂⎛ ⎞ ⎛ ⎞= −⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠
, ,P n T n
v sT P∂ ∂⎛ ⎞ ⎛ ⎞= −⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠
(3.56)
( ), , , j
i
P n i P T n
nsgT n
∂⎛ ⎞∂⎛ ⎞ = −⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠ (3.57)
and ( ), , , j
i
T n i P T n
nvgP n
∂⎛ ⎞∂⎛ ⎞ =⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠ (3.58)
By employing Eq. 3.18
( ), , j
ii P T n
nMM
n∂⎛ ⎞
= ⎜ ⎟∂⎝ ⎠ (3.18)
we can re-write Eqs. 3.57 & 3.58 as follows
,
ii
P n
g sT
∂⎛ ⎞ = −⎜ ⎟∂⎝ ⎠ (3.59)
,
ii
T n
g vP
∂⎛ ⎞ =⎜ ⎟∂⎝ ⎠ (3.60)
225
When comparing with Eqs. 3.10 & 3.9
,P n
g sT
∂⎛ ⎞ = −⎜ ⎟∂⎝ ⎠ (3.10)
,T n
g vP∂⎛ ⎞ =⎜ ⎟∂⎝ ⎠
(3.9)
we can conclude that
“Every equation that provides a linear
relation among thermodynamic
properties of a constant-composition
solution has its counterpart as an
equation connecting the corresponding
partial properties of each species in the
solution”
226
Example In the case of a constant-
composition solution ( ). . 0ii e dn = , we
know that ( ),ig f T P=
Hence,
, ,
i ii
P n T n
g gdg dT dPT P
∂ ∂⎛ ⎞ ⎛ ⎞= +⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠
Combining the above equation
with Eqs. 3.59 & 3.60 results in
i i idg sdT v dP= − + (3.61)
which is in accord with Eq. 2.13
dg sdT vdP= − + (2.13)
227
3.4 Ideal-Gas Mixtures
If n moles of a mixture of ideal
gases contain in a container with a
volume of tV at the temperature of T,
the total pressure of the container
can be calculated using the
following equation:
tnRTPV
= (3.62)
228
and if in moles of species i contain in the
same container, the partial pressure of
species i ( )iP at the same temperature,
T, is as follows:
ii t
nRTPV
= (3.63)
(3.63)/(3.62) gives
i
ti i
i
t
nRTP nV xnRTP n
V
= = =
or i iP x P=
229
Partial volume of species i (ideal gas)
can be written in the form of equation
as follows:
, ,
, ,
, ,
j
j
j
igig
ii T P n
i
T P n
i T P n
nvvn
RTnP
n
RT nP n
⎛ ⎞∂= ⎜ ⎟∂⎝ ⎠
⎛ ⎞⎛ ⎞∂ ⎜ ⎟⎜ ⎟⎝ ⎠= ⎜ ⎟∂⎜ ⎟⎜ ⎟
⎝ ⎠
⎛ ⎞∂= ⎜ ⎟∂⎝ ⎠
Since i jn n n= +∑ , but jn is constant,
we obtain
( ), , , ,j j
i j
i iT P n T P n
n nnn n
⎛ ⎞∂ +⎛ ⎞∂= ⎜ ⎟⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠
∑
( ), , , ,
1j j
ji
i iT P n T P n
nnn n
⎛ ⎞∂⎛ ⎞∂= + =⎜ ⎟⎜ ⎟ ⎜ ⎟∂ ∂⎝ ⎠ ⎝ ⎠
∑ 0
230
Thus,
ig igi i
RTv vP
= =
which illustrates that, in the case of an
ideal-gas mixture
ig igi iv v= (3.64)
The above relation can also be
extended to other thermodynamic
properties:
“A partial molar property of a constituent
species in an “ideal-gas” mixture is equal to
the corresponding molar property of the
species as a pure ideal gas at the same
temperature, but at a pressure equal to its
partial pressure in the mixture”
231
which can be written in the form of
equation as follows:
( ) ( ), ,ig igi i iM T P M T P= (3.65)
3.4.1 For Enthalpy: ( ) ( )=, ,ig ig
i i ih T P h T P
However, we have known (from
Chapter 2) that an enthalpy of an ideal
gas is independent of P
Hence,
( ) ( ) ( ), , ,ig ig igi i i ih T P h T P h T P= =
meaning that
ig igi ih h= (3.66)
232
Applying Eq. 3.28
i iM x M= ∑ (3.28)
to enthalpy, yields
ig ig igi i i ih x h x h= =∑ ∑ (3.67)
This indicates that, for an ideal-gas
solution, the summation of an enthalpy
of each “pure” species is equal to the
enthalpy of the solution
233
3.4.2 For Entropy: Since an entropy of an ideal gas
depends on both T & P (see Chapter 2),
by considering Eq. 2.31 when T is
constant, we obtain
igi p
dT dPds c RT P
= −
ln
igi
dPds RP
Rd P
= −
= −
Integrating the above equation
from P = Pi to P = P yields
0
234
ln
ln
i i
i
P Pig
iP P
P
P
ds Rd P
R d P
= −
= −
∫ ∫
∫
( ) ( ) [ ], , ln lnig igi i i is T P s T P R P P− = − −
( ) ( ), , lnig igi i i
i
Ps T P s T P RP
− = −
but ii
PxP
= i iP x P=
Accordingly,
( ) ( ) 1, , ln lnig igi i i
i i
Ps T P s T P R Rx P x
− = − = −
( ) ( ), , lnig igi i i is T P s T P R x− = (3.68)
235
Applying Eq. 3.65 to entropy yields
( ) ( ), ,ig igi i is T P s T P= (3.69)
Combining Eq. 3.68 with Eq. 3.69 results in
( ) ( ), , lnig igi i is T P s T P R x− = (3.70)
Rearranging Eq. 3.70 gives
( ) ( ), , lnig igi i is T P s T P R x= − (3.71)
Multiplying Eq. 3.71 with xi gives
( ) ( ), , lnig igi i i i i ix s T P x s T P Rx x= − (3.72)
Applying Eq. 3.28 ( )i iM x M= ∑ to Eq. 3.72
yields
( ) ( ), , lnig igi i i i i ix s T P x s T P R x x= −∑ ∑ ∑
( ), lnig igi i i is x s T P R x x= −∑ ∑ (3.73)
236
Rearranging Eq. 3.73 gives
( ) 1, lnig igi i i
i
s x s T P R xx
− =∑ ∑ (3.74)
Note that ( ),ig igi is x s T P−∑ = entropy
change of mixing for ideal gas
Since 1 ix > 1, ( ),ig igi is x s T P−∑ > 0
(positive, +, sign) in agreement
with the 2nd law of thermodynamics
(what does the 2nd law say?)
237
Applying the “relations among
partial properties” to the Gibbs free
energy for an ideal gas
ig ig igg h Ts= − (3.75)
gives
ig ig igi i ig h Ts= − (3.76)
Combining Eq. 3.76 with Eqs. 3.66
& 3.71 yields
( )lnig ig igi i i ig h T s R x= − − (3.77)
Rearranging Eq. 3.77 results in
( ) lnig ig igi i i ig h Ts RT x= − +
lnig igi i i ig g RT xμ= = + (3.78)
238
For an ideal gas when T is constant,
Eq. 2.13
dg vdP sdT= − (2.13)
becomes
igidg vdP
RT dPP
dPRTP
=
=
=
lnigidg RTd P= (3.79)
Integrating Eq. 3.79 yields
( )lnigi ig RT P T= + Γ (3.80)
where ( )i TΓ = integration constant
= f(T)
239
Combining Eq. 3.78 with Eq. 3.80
results in
( )( ) ( )
lnln ln
ln ln
ig igi i i
i i
i i
g g RT xRT P T RT x
T RT x P
= +
= + Γ +⎡ ⎤⎣ ⎦= Γ + +
( ) lnigi i ig T RT x P= Γ + (3.81)
Applying Eq. 3.28 to Eq. 3.81 yields
( ) lnig igi i i i i ig x g x T RT x x P= = Γ +∑ ∑ ∑
(3.82)
240
3.5 Fugacity and Fugacity Coefficient: Pure Species
Re-writing Eq. 3.80
( )lnigi ig RT P T= + Γ (3.80)
for pure & real fluids at constant T
gives
( )lni i ig RT f T= + Γ (3.83)
The property if in Eq. 3.83 is called
a “FUGACITY”
Accordingly, fugacity has the
same unit as pressure
241
(3.83) – (3.80) yields
( ) ( )ln ln
ln
igi i i i i
i
g g RT f T RT P TfRTP
− = + Γ − + Γ⎡ ⎤⎣ ⎦
=
but ig Ri i ig g g− = (see Chapter 2); thus,
lnR ii
fg RTP
=
Note that ii
fP
φ= = FUGACITY
COEFFICIENT
Hence,
lnRi ig RT φ= (3.84)
242
In the case of an ideal gas: if P=
1ii
fP
φ = = ( )ln 1 0Rig RT= =
Rearranging Eq. 3.84 gives
lnRi
igRT
φ = (3.85)
Combining Eq. 3.85 with Eq. 2.67
(see Chapter 2)
( )0
1PRg dPZ
RT P= −∫ (2.67)
yields
( )0
ln 1PR
ii i
g dPZRT P
φ = = −∫ (3.86)
243
In the case of cubic EoS (e.g.,
Redlich-Kwong, Soave-Redlich-Kwong,
& Peng-Robinson EoS), the property Rg
RT
can be written for species i, as follows
( ) ( )ρ= − − − + −ln 1 1Ri
i ig b Z qI ZRT
(2.85a)
Combining Eq. 2.85a with Eq. 3.85
lnRi
igRT
φ = (3.85)
gives
( ) ( )ln ln 1 1R
ii i i
g b Z qI ZRT
φ ρ= = − − − + − (3.87)
244
but, from Eq. 2.95 (See Chapter 2)
B bZ
ρ= (2.95)
or, for species i
i
i
B bZ
ρ= (2.95a)
Eq. 3.87 can, thus, be re-written as
follows:
( ) ( )ln ln 1R
ii i i i
g Z B qI ZRT
φ = = − − − + − (3.88)
245
3.6 Vapour/Liquid Equilibrium (VLE) for Pure Species
When a system consists of liquid (l)
and vapour (v), we can write Eq. 3.83
for each phase, as follows:
( )lnv vi i ig RT f T= + Γ (3.89)
( )lnl li i ig RT f T= + Γ (3.90)
(3.89) – (3.90) yields
ln ln
ln
v l v li i i i
vil
i
g g RT f RT ffRTf
− = −
=
246
At equilibrium,
v li ig g=
or 0v li ig g− =
Thus, this means that
ln 0v
il
i
ff=
or v l sati i if f f= = (3.92)
“For a pure species coexisting
liquid and vapour phases are in
equilibrium when they have the
same T, P, and FUGACITY”
247
Dividing Eq. 3.92 with P results in
v l sat
i i if f fP P P= =
v l sati i iφ φ φ= = (3.93)
which implies that, when two phases
are in equilibrium with each other at
constant T & P, in addition to the fact
that the fugacity of each phase is
equal to each other, their fugacity
coefficients are also identical
248
Example For H2O at a T of 300 oC and for
P up to 10,000 kPa (100 bar), calculate
values of if and iφ using data from steam
tables
Writing Eq. 3.83 for a constant-P system
at P = P gives
( )lni i ig RT f T= + Γ (3.83)
and at P = low P yields
( )* *lni i ig RT f T= + Γ (3.94)
(3.83) – (3.94) results in
**ln i
i ii
fg g RTf
− =
*
*ln i i i
i
f g gRTf−
= (3.95)
249
Writing the following equation
i i ig h Ts= − (3.96)
for a low-P system gives
* * *i i ig h Ts= − (3.97)
(3.96) – (3.97) results in
( ) ( )* * *i i i i i ig g h h T s s− = − − − (3.98)
Dividing Eq. 3.98 with RT yields
( ) ( )* **i i i ii i
h h s sg gRT RT R
− −−= −
Substituting the above Eq. into Eq. 3.95
results in
( ) ( )* *
*ln i i i ii
i
h h s sfRT Rf− −
= − (3.99)
250
Let low P = 6 kPa, and when T = 300 oC
(note that, at low P (& high T as T = 300 oC),
water vapour (H2O) can be assumed to be
an ideal gas; hence, * * 6 kPaif P= = )
h = 3,076.8 kJ/kg & s = 9.5162 kJ/kg-K (by reading from a superheated steam table)
At P = 4,000 kPa (4 MPa) & T = 300 oC
(superheated vapour), we obtain the
following values
h = 2,958.6 kJ/kg & s = 6.3531 kJ/kg-K Substituting corresponding numerical
values into Eq. 3.99 results in
251
[ ]( )
[ ]( )
[ ]( )
*
kJ18.02 2,958.6 3,076.8 kmolln
kJ8.314 300 273 Kkmol-K
kJ18.02 6.3561 9.5162 kmol-K
kJ8.314 kmol-K
6.395
i
i
ff
−=⎛ ⎞ +⎜ ⎟⎝ ⎠
−−
⎛ ⎞⎜ ⎟⎝ ⎠
=
(note that we have to multiply the values of h
& s obtained from the steam table with MW of water
(= 18.02) to convert the units of h & s to be kJ/kmol
& kJ/kmol-K, respectively)
Thus,
* exp(6.395) 598.84i
i
ff= =
( )*598.84 598.84 6 kPa 3,593 kPai if f= = =
and
3,593 kPa 0.8984,000 kPa
ii
fP
φ = = =
252
When P = 10,000 kPa & T = 300 oC
(the system (H2O) is now in the form of
“compressed liquid”), we obtain the
following
h = 1,347.3 kJ/kg & s = 3.2519 kJ/kg-K
Substituting corresponding numerical
values into Eq. 3.99 yields
[ ]( )
[ ]( )
[ ]( )
−=⎛ ⎞ +⎜ ⎟⎝ ⎠
−−
⎛ ⎞⎜ ⎟⎝ ⎠
=
*
kJ18.02 1,347.3 3076.8 kmolln
kJ8.314 300 273 Kkmol-K
kJ18.02 3.2519 9.5162 kmol-K
kJ8.314 kmol-K
7.057
i
i
ff
253
Hence,
= =* exp(7.057) 1,160.96i
i
ff
( )*1,160.96 1,160.96 6 kPa 6,966 kPai if f= = =
and
6,966 kPa 0.69710,000 kPa
ii
fP
φ = = =
It can be observed, from this
Example, that when P is getting higher,
the discrepancy between the values of
if and P is getting larger Also, when P is getting higher, the
value of φi is lower and getting more
and more deviated from unity (i.e. 1)
254
3.7 Fugacity and Fugacity Coefficient: Species in Solutions
Combining Eq. 3.78
lnig ig igi i i ig g RT xμ = = + (3.78)
with Eq. 3.80
( ) lniig
ig T RT P= Γ + (3.80)
gives the following equation:
( )( )ln lnig igi i i ig T RT P RT xμ = = Γ + +
Rearranging the above equation
gives
( ) ( )lnig igi i i ig T RT x Pμ = = Γ + (3.100)
which is the same as Eq. 3.81
255
If this is a “real” solution (can be
either gaseous or liquid solution), Eq.
3.100 can be re-written as follows:
( ) ˆlni i i ig T RT fμ = = Γ + (3.101)
where
if = fugacity of species i in a solution
We have just learned that, if there
are 2 phases (e.g., phases α & β ) co-
existing in equilibrium at given T & P, it
results in the fact that
i if fα β=
256
The above equation can also be
applied to any species in a solution
as follows
ˆ ˆi if fα β=
“Multiple phases at the same
T & P are in equilibrium when
the fugacity of each constituent
species is the same in all phases”
257
We have learned, from Chapter 2,
that
R igM M M= − (2.55)
Hence, (3.101) – (3.100) results in
( )ˆln ln
R ig igi i i i i
i i
g g g
RT f RT x P
μ μ= − = −
= −
ˆ
lnR ii
i
fg RTx P
⎛ ⎞= ⎜ ⎟
⎝ ⎠ (3.102)
Let ˆ ˆ
ˆ i ii
i i
f fx P P
φ = =
Thus,
ˆlnRi ig RT φ= (3.103)
where iφ = fugacity coefficient of
species i in a solution
258
We do the same as did previously
for iφ (see Page 242) and, thus,
obtain
( )0
ˆln 1P
i idPZP
φ = −∫ (3.104)
259
3.8 Generalised Correlations for the Fugacity Coefficient
Combining Eq. 3.86
( )0
ln 1P
i idPZP
φ = −∫ (3.86)
with the following equations
rc
PPP
=
c rP P P= (3.105)
( )c r
c r
dP d P PP dP
=
= (3.106)
results in
260
( )0
ln 1rP
c ri i
c r
P dPZP P
φ = −∫
( )0
ln 1rP
ri i
r
dPZP
φ = −∫ (3.107)
We can write Pitzer et al theorem
of corresponding states
( ) ( )ω= +0 1Z Z Z (1.21)
for species i as follows
( ) ( )ω= +0 1i i iZ Z Z (3.108)
261
Subtracting both sides of Eq. 3.108
with 1 results in
0 11 1i i iZ Z Zω− = − + (3.109)
Combining Eq. 3.107 with Eq. 3.109
gives
( )
( )
( )
φ
ω
φ ω
= −
= − +
= − +
∫
∫
∫ ∫
0
0 1
0
0 1
0 0
ln 1
1
ln 1
r
r
r r
Pr
i ir
Pr
i ir
P Pr r
i i ir r
dPZP
dPZ ZP
dP dPZ ZP P
262
Let
( )0 0
0
ln 1rP
ri i
r
dPZP
φ = −∫
and 1 1
0
lnrP
ri i
r
dPZP
φ = ∫
Thus,
0 1ln ln lni i iφ φ ω φ= +
Rearranging the above equation
yields
( )
( )( )
0 1
0 1
ln ln ln
ln
i i i
i i
ω
ω
φ φ φ
φ φ
= +
⎡ ⎤=⎣ ⎦
( )( )0 1i i i
ωφ φ φ= (3.110)
263
Note that the values of 0iφ and 1
iφ in table
format (Tables A.3.1 and A.3.2) are
included at the end of this Chapter (on
Pages 284-285 and 286-287, respectively)
Example Determine the values of
fugacity coefficient ( iφ ) and fugacity ( if)
of R-134a at 300 oC, and (a) 80 bar and
(b) 284 bar
For R-134a:
374.26 KcT =
40.59 barcP =
0.326ω =
264
(a)
80 bar 1.9740.59 barr
c
PPP
= = =
[ ]300 273 K1.53
374.26 Krc
TTT
+= = =
By performing double interpolations
of ( )φ 0i and ( )φ 1
i appeared in Tables A.3.1
and A.3.2, we obtain
( )φ =0 0.8495i
( )φ =1 1.1828i
Hence,
( )( )0.3260.8495 1.18280.897
iφ =
=
and ( )( )φ= = =0.897 80 bar 71.8 bari if P
265
(b) 284 bar 7.0
40.59 barrc
PPP
= = =
[ ]300 273 K1.53
374.26 Krc
TTT
+= = =
Thus, also by reading from Tables A.3.1
and A.3.2 and performing double
interpolations, we obtain
( )φ =0 0.6866i
( )φ =1 1.5817i Hence,
( )( )0.3260.6866 1.58170.797
iφ =
=
and
( )( )0.797 284 bar226.3 bar
i if Pφ= =
=
266
3.9 The Ideal Solution In the case that we are dealing
with an ideal liquid solution, Eq. 3.78
lnig igi i ig g RT x= + (3.78)
can be re-written for an ideal solution
as follows:
lnidi i ig g RT x= + (3.111)
Differentiating Eq. 3.111 with respect
to T, while P and composition are kept
constant, yields
, ,,
lnidi i i
P x P xP x
g g RT xT T T
⎛ ⎞∂ ∂ ∂⎛ ⎞ ⎛ ⎞= +⎜ ⎟ ⎜ ⎟ ⎜ ⎟∂ ∂ ∂⎝ ⎠ ⎝ ⎠⎝ ⎠
267
Combining the above equation with Eq.
3.59
,
ii
P x
g sT
∂⎛ ⎞ = −⎜ ⎟∂⎝ ⎠ (3.59)
results in
,
lnid ii i
P x
gs R xT
∂⎛ ⎞− = +⎜ ⎟∂⎝ ⎠
and ,
lnid ii i
P x
gs R xT
∂⎛ ⎞= − −⎜ ⎟∂⎝ ⎠ (3.112)
Combining Eq. 3.10
,P x
g sT
∂⎛ ⎞ = −⎜ ⎟∂⎝ ⎠ (3.10)
re-written for species i
,
ii
P x
g sT
∂⎛ ⎞ = −⎜ ⎟∂⎝ ⎠ (3.10a)
with Eq. 3.112 gives
268
( ) lnln
idi i i
i i
s s R xs R x
= − − −
= − (3.113)
Differentiating Eq. 3.111 with respect
to P, while T and composition are kept
constant, yields
, ,,
lnidi i i
T x T xT x
g g RT xP P P
⎛ ⎞∂ ∂ ∂⎛ ⎞ ⎛ ⎞= +⎜ ⎟ ⎜ ⎟⎜ ⎟∂ ∂ ∂⎝ ⎠ ⎝ ⎠⎝ ⎠ (3.114)
Combining Eq. 3.114 with Eq. 3.60
,
ii
T x
g vP
∂⎛ ⎞ =⎜ ⎟∂⎝ ⎠ (3.60)
results in
,
0id ii
T x
gvP
∂⎛ ⎞= +⎜ ⎟∂⎝ ⎠
Note that ln iRT x is a constant
269
By combining the above equation
with Eq. 3.9 re-written for species i
,
ii
T x
g vP
∂⎛ ⎞ =⎜ ⎟∂⎝ ⎠ (3.9a)
we obtain
idi iv v= (3.115)
When we applied the following
equation
g h Ts= −
to an ideal solution, we obtain
id id idi i ig h Ts= −
or
id id idi i ih g Ts= + (3.116)
270
Combining Eq. 3.116 with Eqs. 3.111 &
3.113 gives
[ ] [ ]= + + −
= + =
ln lnidi i i i i
i i i
h g RT x T s R xg Ts h
which indicates that
idi ih h= (3.117)
Applying Eq. 3.28
i ii
M x M= ∑ (3.28)
to an ideal solution gives id id
i ii
M x M= ∑
271
Thus,
ln
ln
id idi i i i i i
i i i i
g x g x g x RT x
x g RT x x
= = +
= +∑ ∑ ∑∑ ∑
(3.118)
lnid idi i i i i is x s x s R x x= = −∑ ∑ ∑ (3.119)
id idi i i iv x v x v= =∑ ∑ (3.120)
id idi i i ih x h x h= =∑ ∑ (3.121)
272
3.10 The Lewis/Randall Rule
When applying Eq. 3.101
( ) ˆlni i i ig T RT fμ = = Γ + (3.101)
to an ideal solution, we obtain
( ) ˆlnid id idi i i ig T RT fμ = = Γ + (3.122)
Combining Eq. 3.83
( ) lni i ig T RT f= Γ + (3.83)
with Eq. 3.111
lnidi i ig g RT x= + (3.111)
yields
273
( ) ( )ˆln ln lnidi i i i iT RT f T RT f RT xΓ + = Γ + +⎡ ⎤⎣ ⎦
Rearranging the above equation
gives
( )
ˆln ln lnln
idi i i
i i
RT f RT f RT xRT x f
= +
=
idi i if x f= (3.123)
Eq. 3.123 = “Lewis/Randall Rule”
“Fugacity of each species in an
ideal solution is proportional to its
mole fraction, where fugacity of
pure species i is a proportionality
constant”
274
Dividing Eq. 3.123 with ix P yields
id
i i i i
i i
f x f fx P x P P
= =
We have defined (see Page 257) that
ˆ
ˆ ii
i
fx P
φ =
and when applying the above definition to
an ideal solution, we obtain
ˆ
ˆid
id i ii
i
f fx P P
φ = =
275
Since
ii
fP
φ =
(see Page 241)
idi iφ φ= (3.124)
(Note: for IDEAL SOLUTION only)
276
3.11 Excess Properties
As well as a residual property
R igM M M= − (2.55)
an excess property indicates how far
a real solution deviates from an ideal
solution, which can be written in the
form of equation as follows
E idM M M= − (3.125)
(3.125) – (2.55) results in
( ) ( )( )
E R id ig
id ig
M M M M M M
M M
− = − − −
= − − (3.126)
277
Since an ideal-gas mixture is an
ideal-gas solution, when we replace ig
in Eq. 3.118
= +∑ ∑ lnidi i i ig x g RT x x (3.118)
with igig , the resulting equation is as
follows:
= +∑ ∑ lnig igi i i ig x g RT x x (3.127)
(by applying Eq. 3.28 to Eq. 3.78)
Eqs. 3.119-3.121 can also be re-
written as a function of igiM in the same
manner as Eq. 3.127 (please try to do it
yourself)
278
Thus, (3.118) – (3.127) yields − = − =∑ ∑ ∑id ig ig R
i i i i i ig g x g x g x g
When performing the same derivation
for Eqs. 3.119-3.121, we obtain the following
general equation for any property id ig ig R
i i i i i iM M x M x M x M− = − =∑ ∑ ∑
(3.128)
When combining Eq. 3.128 with
Eq. 3.126, we obtain
( )E R Ri iM M x M− = − ∑
E R Ri iM M x M= −∑ (3.129)
279
Note that Eq. 3.125 can be applied
to any partial property, as follows:
E idM M M= − (3.130)
280
3.12 The Excess Gibbs Energy and the Activity Coefficient
We can write Eq. 3.101
( ) ˆlni i i ig T RT fμ = = Γ + (3.101)
for an ideal solution, as follows
( ) ˆlnid idi i ig T RT f= Γ + (3.131)
Combining Eq. 3.131 with Eq. 3.123
(Lewis/Radall Rule)
idi i if x f= (3.123)
gives
( ) lnidi i i ig T RT x f= Γ + (3.132)
281
(3.101) – (3.132) results in
ˆ
lnid E ii i i
i i
fg g g RTx f
− = = (3.133)
Let ii
i i
fx f
γ = = activity coefficient of
species i in a solution
Thus,
lnEi ig RT γ= (3.134)
and
lnEi
igRT
γ= (3.135)
282
When applying Eq. 3.28 to Eq. 3.135,
we obtain
lnEEi
i i igg x x
RT RTγ= =∑ ∑ (3.136)
The Nature of Excess Properties
(See Figure 3.4)
• Strongly depend on T
• Weakly depend on P, especially
at moderate T
• Depend on composition, but
the dependence varies from
solution to solution
283
Figure 3.4: Examples of the Nature of Excess Properties
(from Introduction to Chemical Engineering Thermodynamics: 7th ed, by Smith, Van Ness, and Abbott, 2005)
284
Table A.3.1: Values of φ0 as a function of Tr and Pr (from Introduction to Chemical Engineering Thermodynamics:
7th ed, by Smith, Van Ness, and Abbott, 2005)
285
Table A.3.1: Values of φ0 as a function of Tr and Pr (cont.) (from Introduction to Chemical Engineering Thermodynamics:
7th ed, by Smith, Van Ness, and Abbott, 2005)
286
Table A.3.2: Values of φ1 as a function of Tr and Pr (from Introduction to Chemical Engineering Thermodynamics:
7th ed, by Smith, Van Ness, and Abbott, 2005)
287
Table A.3.2: Values of φ1 as a function of Tr and Pr (cont.) (from Introduction to Chemical Engineering Thermodynamics:
7th ed, by Smith, Van Ness, and Abbott, 2005)