PETE 310. Lectures # 6 & # 7 Phase Behavior – Pure Substances (Lecture # 5) Two Component Mixtures Three & Multicomponent Mixtures. Learning Objectives. After completing this chapter you will be able to:
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PETE 310
Lectures # 6 & # 7
Phase Behavior – Pure Substances (Lecture # 5)
Two Component Mixtures
Three & Multicomponent Mixtures
After completing this chapter you will be able to:
Fusion Curve
Critical
2
phases
Point
P
c
Solid
Liquid
(1 phase)
(1 phase)
Pressure
Vapor Pressure
Curve (2 phases)
Vapor (1 phase)
Triple Point
(3 phases)
Sublimation Curve (2 phases)
T
Temperature
c
Single Component Phase Diagram
Critical Point
r
P
l
c
Pressure
Liquid
r
v
Vapor
T
c
Temperature
Vapor Pressure Curve
One point in the
Vapor Pressure Curve
T
)
psia
CP
Tc
Pressure (
2-phase
V
V
L
v
Specific Volume (ft3 / lbm)
d
P
v
Lv
=
T
D
V
dT
Clapeyron equation
Btu/lb-mol
With
DV = VMg-VMl
d
P
v
Lv
V
dT
Lv
d
P
v
P
v
dT
2
R
T
=
T
D
Approximate relation (Clausius - Clapeyron Equation)
=
Calculate how many BTU/day (just from the latent heat of steam) are provided to a reservoir by injecting 6000 bbl/day of steam at 80% quality and at a T=462 oF
Log scale
heavier
Pressure
Temperature
Non-linear scale
1
2
3
4
5
gas
gas
b
V
V
V
=
V
t1
t2
V
t3
t4
t5
V
liquid
liquid
liquid
liquid
liquid
Hg
Hg
Hg
Hg
Hg
>>
P
P
>
P
P
=
P
P
=
P
P
=P
P
1
s
2
s
3
s
4
s
5
s
Ps =saturation pressure
Temperature of Test Constant
T2
Pressure
P
S
T1
V
L
Volume
+
Gas system
open
Oil system
yi(T1,P2)
P1 > P2
zi(T1,P1)
T1,P2
xi(T1,P2)
with
In general
Phase Diagrams for
Binary Mixtures
Zi = fixed
CB
CP
Liquid
CT
Bubble Curve
Pressure
2 Phases
Gas
Dew Curve
Temperature
CP1
Ta
Liquid
P1v
P1v
Bubble Curve
Pressure
2-phases
CP2
Dew Curve
P2v
Vapor
P2v
1
Ta
0
Temperature
x1, y1
Pa
T2s
CP1
Dew Curve
Pressure
2-phases
CP2
Pa
Bubble Curve
T1s
T2s
Temperature
1
T1s
x1, y1
0
A
z
= fix
ed
1
T
= T
CP
a
B
M
P
B
C
Pressure
P
D
y
1
T
0
x
z
1
a
1
1
Temperature
z1=overall mole fraction of [1],y1=vapor mole fraction of [1],x1=liquid mole fraction of [1]
C1
C1
C1
Gas
Gas
Gas
2-phase
2-phase
Liquid
Liquid
nC5
C3
nC5
C3
nC5
C3
p=500 psia
p=14.7 psia
p=380 psia
C1
C1
C1
Gas
Gas
2-phase
2-phase
Liquid
Liquid
Liquid
nC5
C3
nC5
nC5
p=2000 psia
p=2350 psia
p=1500 psia
Pressure Effect
C3
C3
Dilution Lines
Quantitative Representation of Phase Equilibria - Tie (or equilibrium) lines
Quantitative Representation of Phase Equilibria - Tie (or equilibrium) lines
Representation of Multi-Component Phase Behavior with a Pseudoternary Diagram
Miscible Recovery Processes
Solvent2
Solvent1
oil
Find overall composition of mixture made with 100 moles oil "O" + 10 moles of mixture "A".
__________________________
________________________
_______________________
_____________________
___________________
_________________
T=180F
P=200 psia
T=180F
P=14.7 psia
T=180F
P=600 psia
Pressure Effect
Pressure Effect
Pressure Effect
Pressure Effect
T=180F
P=400 psia
C1-C3-C10
O
O
O
O
Pressure Effect
Pressure Effect
Pressure Effect
T=180F
P=4000 psia
T=180F
P=1000 psia
T=180F
P=2000 psia
T=180F
P=3000 psia
T=180F
P=1500 psia
O
O
O
O
O
Pressure Effect
Temperature Effect
Temperature Effect
Temperature Effect
Temperature Effect
T=100F
P=2000 psia
T=200F
P=2000 psia
T=150F
P=2000 psia
T=300F
P=2000 psia
O
O
O
O
Temperature Effect
Temperature Effect
Temperature Effect
Temperature Effect
T=400F
P=2000 psia
T=450F
P=2000 psia
T=350F
P=2000 psia
O
O
O
Temperature Effect
1-Phase
1-Phase
CP
Bubble-Curve
60%
0%
Reservoir Pressure
20%
2-Phase
Dew-Curve
Reservoir Temperature
t
t
1
Production
Production
t
2
2
Gas
Gas
Pressure
Injection
Injection
t
t
3
3
Temperature