# Performance Evaluation of Refrigeration Units in Natural Gas Liquid Extraction Plant

Authors: Awajiogak Anthony Ujile; Dirina Amesi
Journal: Journal of Thermodynamics
 (2014)

---

## Abstract

This paper has applied thermodynamics principles to evaluate the reliability of 390 m3/hr natural gas processing plant. The thermodynamics equations were utilized in the evaluation, characterization, and numerical simulation of key process parameters in natural gas liquid extraction plant. The results obtained show the comparison of the coefficient of performance, compression ratio, isentropic work, actual work, electrical power requirements, cooling water consumption in intercoolers, compressor power output, compressor capacity, and isentropic, volumetric, and mechanical efficiency of the two-stage refrigeration unit with a flash gas economizer and these were compared with the designed specifications. The second law of thermodynamics was applied in analyzing the refrigeration unit and the result shows that exergetic losses or lost work due to irreversibility falls within operating limit that is less than 1.0%. Similarly, the performance of expansion turbine (expander) parameters was monitored and the results indicate a considerable decrease in turbine efficiencies as the inlet gas pressure increases resulting in an increased power output of the turbine leading to a higher liquefaction rate.


---

## Body

## 1. Introduction

The production and availability of natural gas liquid depend largely on the supply of raw natural gas from production wellhead and the operating conditions of the process unit that make up the extraction plant. Most gas processing plants are faced with problems ranging from inadequate supply, poor facility performance, and human factors. These problems can lead to low productivity of natural gas liquids and reduction in gas quality which could result in shutting down of the plant. Poor facilities such as inadequate electricity supply and processed water supply used in process equipment also lead to intermittent operations and malfunction of process equipment such as pumps, compressors, and valves if they are not adequately checked.Human factors may also result from the inability of gas plant operators to monitor thermodynamics parameters such as the pressure, flow rates, and temperature on process equipment which could result in loss of data in control room and unintended activation or deactivation of process devices and reduce the plant efficiency. In spite of the fact that these thermodynamics parameters are monitored daily in a gas plant, there are problems of low gas feed inlet pressure and insufficient gas flow rate. These have resulted in low volume of natural gas liquids produced, the extracted natural gas liquids not attaining the expected cryogenic temperature requirement, and variation in gas quality discharging from the outlet of natural gas liquid extraction unit bottom product.If the available inlet gas pressure is low, it can result in compressor system suction pressure falling below atmospheric pressure. This can also lead to air leakages into the compressor system, contributing to pulsation, corrosion, and low heating value of natural gas. In order to solve these problems, performance evaluation of the process units in natural gas liquids extraction using thermodynamics principles is necessary to ensure that these problems are minimized.It is seen from literature survey that several papers have been published focusing on thermodynamic analysis of a gas turbine power plant.Rahman et al. [1] and Taniguchi and Miyamae [2] carried out the study on the effects of ambient temperature and ambient pressure as well as temperature of exhaust gases on performance of gas turbine. Khaliq and Kaushik [3] studied the efficiency of a gas turbine cogeneration system with heat recovery steam generator.Keith and Kenneth [4] developed a new method of applying overall plant material balance equation to determine the performance of a natural gas processing plant. Jibril et al. [5] studied the simulation of expansion turbine (expander) for recovery of natural gas liquids from natural gas stream gas using HYPRO TECH’s HYSYS process simulation software. Donnelly et al. [6] carried out researches on process simulation and optimization of cryogenic operations using multistream brazed aluminum heat exchangers. Ganapathy et al. [7] studied the energy analysis of operating lignite fired thermal power plant. Design methodology for parametric study and thermodynamic performance evaluation of natural gas process plant has been developed. Refrigeration unit and expansion turbine unit which are the major components of the plant were evaluated. The expansion of natural gas through an expansion turbine with efficiencies shows a very good performance Ujile and Alawa [8]. The comparison between the energy losses and the energy losses of the components unit were investigated.This paper examined the reliability of a gas plant which is the ability of a plant to maintain a stable efficiency with respect to time using thermodynamics equations.


## 2. Methodology/System Descriptions

### 2.1. Propane Refrigeration Unit

The simulation of process units in propane refrigeration cycle involves the applications of thermodynamics principles to the following.(i)
Calculate the amount of heat added to or removed from process streams.
(ii)
Estimate the power requirements for process equipment such as pumps, compressors, and turbine.
(iii)
Evaluate the performance of a flash separator at various temperatures and pressures.
(iv)
Determine the bubble and dew point temperature associated with distillation and bottom products.A systematic diagram of propane refrigeration cycle is shown in Figure1. The refrigerant passes through the scrubber into the first stage compressor at 1.9 bar as saturated vapor where it mixes up with the vapor from the economizer unit. It is compressed to the inlet of the second stage compressor at 2.5 bar and discharges at 5.0 bar into the condenser as superheated vapor. It leaves the condenser at 4.7 bar and enters the first expansion valve and from the expansion valve into an economizer drum where it flashes at an intermediate pressure of 3.3 bar. The vapour phase with the economizer at the top mixes up the vapour from the first stage compressor, while the liquid discharges at the bottom and enters the second expansion valve into the chiller at a pressure of 2.5 bar. The process gas (natural gas) flows inside the tubes connected to the chiller at 41°C and countercurrently exchanges heat and gives up its energy with the liquid refrigerant surrounding the tubes. The refrigerant boils up and leaves the chiller space as saturated vapor to be recompressed again.Figure 1
Process flow diagram of propane refrigeration of natural gas with application of Hysys software.


### 2.2. Expansion Turbine Unit

A turbo expander or an expansion turbine is a centrifugal or axial flow turbine through which a high pressure gas is expanded to produce useful work that is used to drive a compressor. Because work is extracted from the expanding high pressure gas, the expansion is an approximation by an isentropic process (a constant entropy process).In the process of producing work, the expander lowers the bulk stream temperature which could result in partial liquefaction of the bulk stream (natural gas).A systematic diagram of an expansion turbine (expander) is presented in Figure2. The feed gas enters the gas treating unit after which it is cooled firstly in a gas-to-gas heat exchanger and secondly the propane chiller. The condensed liquid is removed in a separator and the gas from the separator is cooled further in the low temperature gas-to-gas heat exchanger and fed into a second cooled separator. Gas from the cooled separator expands through the expansion turbine to the pressure at the top of the demethanizer which varies from 100 to 450 bar. During the expansion, condensate is formed and the expander lowers the pressure of the inlet gas value to the demethanizer pressure of the range 100–450 bar.Figure 2
Flow diagram of expander process.Thermodynamics Performance Parameters of Propane Refrigeration Unit. The relevant parameters required for thermodynamics performance evaluation of propane refrigeration of natural gas may be considered as follows.Coefficient of Performance. This is defined as the ratio of the heat absorbed (Q
in) by the refrigerant while passing through the chiller to the work input (
W
in
) required compressing the refrigerant in the compressor. This is mathematically expressed as [9, 10]
(1)
COP
=
Q
in
W
in
,
but
(2)
W
in
=
W
comp1
+
W
comp2
=
(
1
-
X
G
)
(
H
B
-
H
A
)
+
M
C
(
H
E
-
H
D
,
MIX
)
,
COP
=
(
1
-
X
G
)
M
C
(
H
A
-
H
I
)
(
1
-
X
G
)
(
H
B
-
H
A
)
+
M
C
(
H
E
-
H
D
,
MIX
)
.
Refrigeration Capacity. The refrigeration capacity determines the rate of circulation of the refrigerant which, in turn, determines the design and size of various units such as condenser, compressor, evaporator (chiller), and expansion valves. This is expressed by the following equation:
(3)
R
c
=
M
C
(
H
A
-
H
I
)
210
KJ
/
min
⁡
.
The mass flow rate of cooling water is calculated as follows:
(4)
M
CW
=
Q
C
p
CW
Δ
T
.
The overall performance of a compressor is affected mainly by the inlet pressure and the interstage cooler efficiency.The simulation of process units in propane refrigeration resulted in loss of energy on the system. The second availability balance was applied to calculate the energy losses or lost work due to irreversibility of the process. The thermodynamics equations applied on each of the process units are as follows [10].Compressor unit:(5)
L
W
=
M
C
[
(
H
A
-
T
o
S
A
)
]
-
(
H
B
-
T
o
S
B
)
-
W
E
;condenser unit:(6)
L
W
=
T
o
[
M
C
(
S
C
-
S
B
)
]
+
M
CW
S
CW
(
out
)
-
S
CW
(
in
)
,
M
CW
=
M
C
[
H
E
-
H
F
H
CW
(
out
)
-
H
CW
(
in
)
]
;expansion valve:(7)
L
W
=
M
C
T
o
(
S
B
-
S
C
)
,
L
W
=
M
C
T
o
[
(
S
A
-
S
D
)
-
(
H
A
-
H
D
T
i
)
]
.Refrigerant chiller: the chiller is the unit where the process gas (natural gas) gives up its energy to the liquid refrigerant. The refrigerating effect which is the amount of heat absorbed by refrigerant or removed from the refrigerated space is expressed as(8)
Q
in
=
(
1
-
X
G
)
M
C
(
H
A
-
H
I
)
.The fraction of refrigerant vaporized in the chiller is determined from enthalpy balance as follows:(9)
M
C
(
H
H
)
L
=
M
C
X
V
(
H
I
)
+
M
C
(
1
-
X
v
)
(
H
I
)
L
,
where X
v is the mole fraction of refrigerant that evaporates as it throttles to the economizer unit.Expansion Turbine Unit. The relevant thermodynamics parameters applied in expansion turbine unit in a gas plant are as follows.(i)
Isentropic Turbine Efficiency. This is defined as the ratio of turbine actual work output to the work output that would be achieved if the process between the inlet and outlet pressure was isentropic. By definition [11],
(10)
η
E
=
h
1
-
h
2
a
h
1
-
h
2
,
S
.
(ii)
Isentropic and Actual Work. The isentropic work of a turbine is the work done by the turbine during the constant entropy whereas actual work is the gross work of a turbine:
(11)
W
act
=
m
(
h
2
-
h
1
)
,
W
is
=
-
m
(
h
1
-
h
2
,
S
)
.
(iii)
Power Recovery. The expander gas power recovery is the output power of the turbine list to drive the compressor. By definition,
(12)
P
g
=
-
η
m
(
h
1
-
h
2
,
S
)
.
(iv)
Theoretical and Actual Discharge Temperature. The discharge and actual temperatures of a turbine are expressed by the following equations [11, 12]:
(13)
T
2
′
=
T
1
(
p
2
p
1
)
(
k
-
1
)
/
k
,
T
2
=
T
1
+
T
1
[
(
p
2
p
1
)
(
K
-
1
)
/
K
-
1
]
η
E
.The results obtained from the evaluation with the above equations are shown in graphical form in Figures 3 and 4.Figure 3
Pressure enthalpy diagram of a propane refrigeration cycle.Figure 4
Temperature entropy diagram of a propane refrigeration cycle.


## 2.1. Propane Refrigeration Unit

The simulation of process units in propane refrigeration cycle involves the applications of thermodynamics principles to the following.(i)
Calculate the amount of heat added to or removed from process streams.
(ii)
Estimate the power requirements for process equipment such as pumps, compressors, and turbine.
(iii)
Evaluate the performance of a flash separator at various temperatures and pressures.
(iv)
Determine the bubble and dew point temperature associated with distillation and bottom products.A systematic diagram of propane refrigeration cycle is shown in Figure1. The refrigerant passes through the scrubber into the first stage compressor at 1.9 bar as saturated vapor where it mixes up with the vapor from the economizer unit. It is compressed to the inlet of the second stage compressor at 2.5 bar and discharges at 5.0 bar into the condenser as superheated vapor. It leaves the condenser at 4.7 bar and enters the first expansion valve and from the expansion valve into an economizer drum where it flashes at an intermediate pressure of 3.3 bar. The vapour phase with the economizer at the top mixes up the vapour from the first stage compressor, while the liquid discharges at the bottom and enters the second expansion valve into the chiller at a pressure of 2.5 bar. The process gas (natural gas) flows inside the tubes connected to the chiller at 41°C and countercurrently exchanges heat and gives up its energy with the liquid refrigerant surrounding the tubes. The refrigerant boils up and leaves the chiller space as saturated vapor to be recompressed again.Figure 1
Process flow diagram of propane refrigeration of natural gas with application of Hysys software.


## 2.2. Expansion Turbine Unit

A turbo expander or an expansion turbine is a centrifugal or axial flow turbine through which a high pressure gas is expanded to produce useful work that is used to drive a compressor. Because work is extracted from the expanding high pressure gas, the expansion is an approximation by an isentropic process (a constant entropy process).In the process of producing work, the expander lowers the bulk stream temperature which could result in partial liquefaction of the bulk stream (natural gas).A systematic diagram of an expansion turbine (expander) is presented in Figure2. The feed gas enters the gas treating unit after which it is cooled firstly in a gas-to-gas heat exchanger and secondly the propane chiller. The condensed liquid is removed in a separator and the gas from the separator is cooled further in the low temperature gas-to-gas heat exchanger and fed into a second cooled separator. Gas from the cooled separator expands through the expansion turbine to the pressure at the top of the demethanizer which varies from 100 to 450 bar. During the expansion, condensate is formed and the expander lowers the pressure of the inlet gas value to the demethanizer pressure of the range 100–450 bar.Figure 2
Flow diagram of expander process.Thermodynamics Performance Parameters of Propane Refrigeration Unit. The relevant parameters required for thermodynamics performance evaluation of propane refrigeration of natural gas may be considered as follows.Coefficient of Performance. This is defined as the ratio of the heat absorbed (Q
in) by the refrigerant while passing through the chiller to the work input (
W
in
) required compressing the refrigerant in the compressor. This is mathematically expressed as [9, 10]
(1)
COP
=
Q
in
W
in
,
but
(2)
W
in
=
W
comp1
+
W
comp2
=
(
1
-
X
G
)
(
H
B
-
H
A
)
+
M
C
(
H
E
-
H
D
,
MIX
)
,
COP
=
(
1
-
X
G
)
M
C
(
H
A
-
H
I
)
(
1
-
X
G
)
(
H
B
-
H
A
)
+
M
C
(
H
E
-
H
D
,
MIX
)
.
Refrigeration Capacity. The refrigeration capacity determines the rate of circulation of the refrigerant which, in turn, determines the design and size of various units such as condenser, compressor, evaporator (chiller), and expansion valves. This is expressed by the following equation:
(3)
R
c
=
M
C
(
H
A
-
H
I
)
210
KJ
/
min
⁡
.
The mass flow rate of cooling water is calculated as follows:
(4)
M
CW
=
Q
C
p
CW
Δ
T
.
The overall performance of a compressor is affected mainly by the inlet pressure and the interstage cooler efficiency.The simulation of process units in propane refrigeration resulted in loss of energy on the system. The second availability balance was applied to calculate the energy losses or lost work due to irreversibility of the process. The thermodynamics equations applied on each of the process units are as follows [10].Compressor unit:(5)
L
W
=
M
C
[
(
H
A
-
T
o
S
A
)
]
-
(
H
B
-
T
o
S
B
)
-
W
E
;condenser unit:(6)
L
W
=
T
o
[
M
C
(
S
C
-
S
B
)
]
+
M
CW
S
CW
(
out
)
-
S
CW
(
in
)
,
M
CW
=
M
C
[
H
E
-
H
F
H
CW
(
out
)
-
H
CW
(
in
)
]
;expansion valve:(7)
L
W
=
M
C
T
o
(
S
B
-
S
C
)
,
L
W
=
M
C
T
o
[
(
S
A
-
S
D
)
-
(
H
A
-
H
D
T
i
)
]
.Refrigerant chiller: the chiller is the unit where the process gas (natural gas) gives up its energy to the liquid refrigerant. The refrigerating effect which is the amount of heat absorbed by refrigerant or removed from the refrigerated space is expressed as(8)
Q
in
=
(
1
-
X
G
)
M
C
(
H
A
-
H
I
)
.The fraction of refrigerant vaporized in the chiller is determined from enthalpy balance as follows:(9)
M
C
(
H
H
)
L
=
M
C
X
V
(
H
I
)
+
M
C
(
1
-
X
v
)
(
H
I
)
L
,
where X
v is the mole fraction of refrigerant that evaporates as it throttles to the economizer unit.Expansion Turbine Unit. The relevant thermodynamics parameters applied in expansion turbine unit in a gas plant are as follows.(i)
Isentropic Turbine Efficiency. This is defined as the ratio of turbine actual work output to the work output that would be achieved if the process between the inlet and outlet pressure was isentropic. By definition [11],
(10)
η
E
=
h
1
-
h
2
a
h
1
-
h
2
,
S
.
(ii)
Isentropic and Actual Work. The isentropic work of a turbine is the work done by the turbine during the constant entropy whereas actual work is the gross work of a turbine:
(11)
W
act
=
m
(
h
2
-
h
1
)
,
W
is
=
-
m
(
h
1
-
h
2
,
S
)
.
(iii)
Power Recovery. The expander gas power recovery is the output power of the turbine list to drive the compressor. By definition,
(12)
P
g
=
-
η
m
(
h
1
-
h
2
,
S
)
.
(iv)
Theoretical and Actual Discharge Temperature. The discharge and actual temperatures of a turbine are expressed by the following equations [11, 12]:
(13)
T
2
′
=
T
1
(
p
2
p
1
)
(
k
-
1
)
/
k
,
T
2
=
T
1
+
T
1
[
(
p
2
p
1
)
(
K
-
1
)
/
K
-
1
]
η
E
.The results obtained from the evaluation with the above equations are shown in graphical form in Figures 3 and 4.Figure 3
Pressure enthalpy diagram of a propane refrigeration cycle.Figure 4
Temperature entropy diagram of a propane refrigeration cycle.


## 3. Results and Discussion

The results on the refrigeration unit of a gas plant were obtained using theP-S and T-S diagrams.The two-stage compression refrigeration system in Figures3 and 4 operates with a pressure range of 1.9 and 5.0 bar. The refrigerant enters the first stage compressor at a suction pressure of 1.9 bar with enthalpy and entropy values of 2704 KJ/kg and 7.145 KJ/kg·K, respectively. It discharges into a mixer where it mixes up with the vapor leaving the top of the flash economizer. The refrigerant is compressed to the second stage compressor operating with a suction pressure of 2.5 bar with enthalpy and entropy values of 2716.4 KJ/kg and 7.052 KJ/kg·K, respectively, and discharges at the condenser inlet pressure of 5.0 bar, where −17,386.7 J/kg of heat is rejected to the surrounding. The enthalpy and entropy values of the condenser as a saturated vapour at a pressure of 4.7 bar were observed to be 630 KJ/kg and 1.8363 KJ/kg·K, respectively. The refrigerant is throttled to a flash economizer at an intermediate pressure of 3.3 bar. During flashing 0.0034 kg/s of vapor evaporates from the economizer drum while 0.1305 kg/s of liquid is throttled to the chiller at a pressure of 1.9 bar with enthalpy and entropy values of 575.5 KJ/kg and 1.8545 KJ⁄kg·K, respectively. The process gas (natural gas) countercurrently exchanges heat and gives up its energy to the liquid refrigerant at a temperature of 41°C. The result of the two-stage compression refrigeration is summarized in Table 1.Table 1
Summary of two-stage compression refrigeration.
Parameters
Units
1st stage compressor
2nd stage compressor
Suction pressure
bar
1.9
2.5
Discharge pressure
bar
2.5
5.0
Compression ratio
—
1.316
1.414
Isentropic work of compression
J/kg
20,644.25
22,094.91
Actual work of compression
J/kg
20,644.25
21,872.85
Isentropic efficiency
%
48.56
51.98
Mechanical efficiency
%
20.71
46.51
Volumetric efficiency
%
55.0
46.7
Actual power requirement
KW
0.0969
0.0960
Cooling water consumption in intercoolers
m3/s
7.2612
19.282
Compressor capacity
m3/s
2.1566
2.1096
Work input in comp 1 and comp 2
J/kg
273.14
273.14
Work output
J/kg
1197.89
2414.11The process parameters of other auxiliary units in propane refrigeration plant are shown in Table2.Table 2
Process parameters of other auxilliary units.
Parameters
Unit
Condenser
Economizer
Expansion valve 1
Expansion valve 2
Refrigerant chiller
Suction pressure
bar
5.0
3.3
4.7
3.3
2.3
Discharge pressure
bar
4.7
—
3.3
1.9
1.9
Heat load
J/kg
−17,386.7
5733.78
—
—
17,036.04
Mass flow rate of vapor—economizer
kg/s
—
0.0034
—
—
—
Mass flow rate of liquid—economizer
kg/s
—
0.1305
—
—
—
Mass flow rate of cooling water—condenser
kg/s
6.72
—
—
—
—
Joule Thompson coefficient
—
—
—
8.57
12.86
—
Mole fraction of liquid remaining in chiller
—
0.035
0.00014
Mole fraction of vapor evaporated in chiller
—
0.025
0.025
—
0.045
Mass flow rate of liquid—condenser accumulator
kg/s
0.1339The energy balance of the propane refrigeration unit obtained from the evaluation based on the equations highlighted for the analysis is shown in Table3.Table 3
Energy balance propane refrigeration unit.
Process units
Energy gain (KJ/kg)
Energy lost (KJ/kg)
% of lost work
Compressor 1
12.30
−334.28
−0.015
Compressor 2
32.11
−501.45
−0.023
Condenser
—
12483.89
0.06
Expansion valve JT-1
—
12495.54
0.06
Expansion valve JT-2
—
−1435547.8
6.62
Economizer drum
5733.78
—
—
Refrigerant chiller
17036.04
−1242710.43
−5.73
Total
22814.23
216981.07
0.972By the design conditions, the centrifugal compressors used in compressing the refrigerant should operate with a pressure ratio of 1.2 : 1 and 1.4 : 1, isentropic efficiency of 70–80%, volumetric efficiency of 60–89%, and mechanical efficiency of 20–50%. By analytical method, the pressure ratio was found to be 1.316 and 1.414; the isentropic efficiency was found to be 48.56% and 51.97%; the volumetric efficiency was found to be 55.0% and 46.7% for the first and second stage compressors, respectively, while the mechanical efficiencies are 57.7% and 46.51%, respectively. The refrigeration cycle was operating with an overall coefficient of performance of 62.37 with a refrigerating capacity of 4,922.2 tons after examining the performance of other auxiliary units within the systems. Tables1, 2, and 3 show values obtained from the evaluation. The Kelvin-Planck statement of the second law of thermodynamics tells us that it is impossible to have a heat engine that will convert all the heat received from the high temperature source, Q
H, into useful work in a thermodynamic cycle. It is necessary to reject part of the received heat to the low temperature source, Q
L. In other words, it is impossible to have a 100% efficiency heat engine as corroborated by Kumar et al. [13] and José and Simões-Moreira [14].


## 4. Conclusion

The thermodynamics equations were applied to construct Figures3 and 4 which determine the performance of the plant. The recorded efficiencies ranging from 63.92% to 77% have shown that the overall performance has deviated from the design efficiency. This condition may increase the operational cost of the plant.The following recommendations are highlighted to ensure optimum efficiency and reliability of NGL plant.(i)
The feed gas must be free from CO2 and water. This affects plant efficiency and operations if not properly checked by freezing the fittings, valves, and other associated equipment.
(ii)
The inlet strainer differential pressure must not be high; otherwise the expander will trip off on high differential pressure.
(iii)
The refrigeration unit must be operated within the operating and design conditions to avoid overfreezing or warming of the demethanizer column.
(iv)
There is need for proper insulation of piping system within the NGL extraction plant. The reason is not to allow the surrounding heat to enter the system, thereby warming the system, and there may be freezing out of the plant.
(v)
Proper sizing of the process line using the various line balance methods to compare the amount of natural gas entering the process plant with the amount put in should be adopted at the design stage of the process plant.



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*Source: 863408-2014-03-25.xml*