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**Performance of a 270 MW Gas Power Plant Using Exergy and Heat Rate** ()

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*Energy and Power Engineering*,

**11**, 15-34. doi: 002.

1. Introduction

The Applied Energy Services (AES) Corporation barge-mounted gas turbine power plants located at Egbin, about 40 km North East of Lagos in Nigeria are the first Independent Power Plant (IPP) in the country with a total installed generating capacity of 270 MW (9 nos. × 30 MW). Each gas turbine drives a generator with an output voltage of 11.3 kV that is stepped up to a terminal voltage of 132 kV before connection to the National Grid. The power plants were brought to the site in 2001. After more than 15 years of operation, it is reasonable to evaluate the performance of the major components of the power plants.

The concept of Exergy of a system has been defined by Kotas [1] , Dincer et al. [2] , Egware and Obanor [3] and, Cengel and Boles [4] as the maximum shaft work that can be obtained from a system at a given state in a specified reference environment. Kotas [1] further highlighted the use of exergy in defining the criteria of performance in thermal plants. Exergy analyses of gas turbine power plants at different locations have also been reported by Ebadi and Gorji-Bandpy [5] , Rosen and Bulucea [6] .

Ali and Mohammad [7] also carried out exergy and exergo-economic analyses of a gas turbine power generating system. The results of the load variation of the gas turbine show that a reduction in gas turbine load results in a decrease in the exergy efficiency of the cycle as well as that of all the components. The advantage of using exergy analysis to identify possible areas of reduction in thermodynamic losses and improvement in efficiencies of major components of electrical power technologies and systems including gas turbine power plants are therefore well documented in the literature. The primary objective of the present study is threefold:

1) To analyze the thermodynamic performance of the major components of three operational gas power plants, each with a rated capacity of 30 MW but from different Original Equipment Manufacturers (A, B and C) using both energy and exergy analysis,

2) To identify and quantify the exergy efficiency of the various components of each plant, and

3) To establish the relationship between the heat rate and the energy and exergy efficiencies of the plant.

2. Methodology

2.1. Data Acquisition

The study made use of the operational data of each of the three power plants. These include the daily records of the performance of each barge (A, B or C), mass flow of fuel, temperature and pressure at various states during generation (see Tables 1-3). Relevant plant and working fluid parameters, such as, air and fuel, specific capacities, relative gas constants and other constants were obtained from appropriate thermodynamic table [8] . The rated conditions are classified into cold rated condition and hot rated condition. The cold rated condition is

Table 1. Operational data for the exergy analysis of the 30 MW gas power plant, A, at 90% MCR.

Table 2. Operational data for the exergy analysis of the 30MW as power plant, B, at 90% MCR.

Table 3. Operational data for the exergy analysis of the 30 MW as power plant, C, at 90% MCR.

when the ambient temperature is 25˚C (see Table 1) and it is said to be hot rated if the ambient temperature is 37˚C (see Table 2).

2.2. Process Description and Isentropic Efficiencies of Major Components

Figure 1 illustrates the schematic flow diagram of a typical 30 MW gas power plant while Figure 2 shows the corresponding T-S diagram, that is, based on the Brayton thermodynamic cycle. The major components of the plants are: 1) the air compressor, 2) the combustion chamber and 3) the gas turbine units.

At state point 1, the compression phase is initiated as air is drawn into the compressor at ambient temperature, T_{1} and atmospheric pressure, P_{1} or PA. It is compressed by a multi-stage axial flow type compressor to an increased pressure, P_{2} and temperature, T_{2}. The compressed air flows into the combustor at state point 2, where it is mixed with the fuel and burned at a constant pressure.

Figure 1. Flow diagram of AES 30 MW gas turbine power plant.

Figure 2. T-S Diagram for the AES gas turbine power plant.

At state point 3 the resulting hot gas, having the highest temperature, T_{3} enters the turbine nozzle and is expanded through turbine section, producing mechanical power by rotating the shaft, which is connected to the generator for electric power generation. At state point 4, the exhaust gases are expanded back to atmospheric pressure, P_{4} (or PA) and exhaust temperature, T_{4}.

In the ideal Brayton cycle, processes 1 - 2 s and 3 - 4 s are isentropi, with P_{2} = P_{3} and P_{4} = P_{1}.

Hence,

${T}_{2s}/{T}_{1}={\left({P}_{2}/{P}_{1}\right)}^{\left(k-1\right)/k}={\left({P}_{3}/{P}_{4}\right)}^{\left(k-1\right)/k}={T}_{3}/{T}_{4s}$ (1)

where k = ratio of specific heat capacities.

The isentropic efficiencies of air compressor (−η_{AC}) and of gas turbine (η_{GT}) are obtained from

${\eta}_{AC}=\left({T}_{2s}\u2013{T}_{1}\right)/\left({T}_{2}-{T}_{1}\right)$ and ${\eta}_{GT}=\left({T}_{3}-{T}_{4}\right)/\left({T}_{3}-{T}_{4s}\right)$ (2)

3. General Exergy Balance for the Control Volume of the Gas Power Plant

The statement of the General Exergy balance for the control volume in Figure 3 (an open system) states that the exergy change of a system during a process is equal to the difference between the net exergy transfer through the system

Figure 3. Control volume for the exergy analysis of AES gas power plant.

boundary by heat, work, mass flow and the exergy destroyed within the system the exergy destroyed within the system boundary as a result of ireversibility. Thus, we can write:

$\begin{array}{l}\text{Net Exergy transfer}\left(\text{by heat},\text{work and mass}\right)\\ \text{\hspace{0.05em}}-\text{Exergy destroyed consumption}\\ =\text{Change in Exergy of the system}\end{array}$ (3)

Thus exergy, a measure of energy quality or work potential, is consumed as a result of irreversibilities.

On the basis of Equation (3) we can write:

$\left({E}_{\text{in}}-{E}_{\text{out}}\right)-{E}_{\text{destroyed}}=\Delta {E}_{\text{system}}$ (4)

where,

(E_{in} − E_{out}) = Net exergy transfer (by heat, work and mass).

E_{destroyed} = Exergy destruction in the system.

∆E_{system} = Change in exergy of the system.

The above Equation (4) can also be expressed as:

${E}_{\text{heat}}-{E}_{\text{work}}+{E}_{\text{mass,in}}-{E}_{\text{mass,out}}-{E}_{\text{destroyed}}={E}_{2}\u2013{E}_{1}$ (5)

where

Exergy transfer by heat, ${E}_{\text{heat}}=\Sigma \left(1-{T}_{0}/{T}_{C}\right){Q}_{C}.$

Exergy transfer by work, ${E}_{\text{work}}=W-{P}_{0}\left({V}_{j}-{V}_{i}\right).$

Exergy transfer by mass into the system, ${E}_{\text{mass,in}}=\Sigma {m}_{\text{in}}\psi .$

Exergy transfer by mass out of the system, ${E}_{\text{mass,out}}=\Sigma {m}_{\text{out}}\psi .$

Substituting the above relations in Equation (5), the exergy balance for a control volume (Figure 3) is,

$\begin{array}{l}\Sigma \left(1-{T}_{0}/{T}_{C}\right){Q}_{C}-\left[W-{P}_{0}\left({V}_{j}-{V}_{i}\right)\right]+\Sigma {m}_{\text{in}}\psi -\Sigma {m}_{\text{out}}\psi -{E}_{\text{destroyed}}\\ =\left({E}_{2}-{E}_{1}\right)cv\end{array}$ (6)

where
$\psi $ is the exergy content for a flow stream and it is given as
$\psi =\left(h-{h}_{0}\right)-{T}_{0}\left(s-{s}_{0}\right)+{v}^{2}/2+{g}_{acc}\ast z$ and P_{0}, h_{0}, T_{0}, s_{0}, are the properties of the system evaluated at the dead state (i.e. the conditions of the environment).

Q_{C} is the heat transfer through the boundary at temperature T_{C} and location c.

m_{in} and m_{out} are the mass flowrate of working fluid at the inlet and exit locations of the system (gas turbine power plant unit).

From Equation (6), W is the boundary work and may be written as:

$W=Q-\Delta U=Q-m\left({u}_{j}-{u}_{i}\right)$

while $W-{P}_{0}\left({V}_{j}-{V}_{i}\right)$ is the useful work, subscripts i and j denote the initial and final states of the system respectively during the process.

V_{i} and V_{j} are the respective volumes at states i and j.

In the rate form, we can write

$\Sigma \left(1-{T}_{0}/{T}_{C}\right){\stackrel{\dot{}}{Q}}_{C}-\left[\stackrel{\dot{}}{W}-{P}_{0}\text{d}V/\text{d}t\right]+\Sigma {\stackrel{\dot{}}{m}}_{\text{in}}\psi -\Sigma {\stackrel{\dot{}}{m}}_{\text{out}}\psi -{E}_{\text{destroyed}}=\text{d}E/\text{d}t$ (7)

For steady flow process and single stream in the case of turbine and compressor, V/dt = 0 and dE/dt = 0.

Hence, the rate form of the general exergy balance in Equation (3) above reduces to:

$\Sigma \left(1-{T}_{0}/{T}_{C}\right){\stackrel{\dot{}}{Q}}_{C}-\left[\stackrel{\dot{}}{W}-{P}_{0}\text{d}V/\text{d}t\right]+\Sigma {\stackrel{\dot{}}{m}}_{\text{in}}\psi -\Sigma {\stackrel{\dot{}}{m}}_{\text{out}}\psi -{E}_{\text{destroyed}}=0$

Or

$\stackrel{\dot{}}{W}=\Sigma \left(1-{T}_{0}/{T}_{C}\right){\stackrel{\dot{}}{Q}}_{C}+\Sigma \stackrel{\dot{}}{m}\left({\psi}_{\text{in}}-{\psi}_{\text{out}}\right)-{E}_{\text{destroyed}}$ (8)

Substituting the exergy content $\psi =\left(h-{h}_{0}\right)-{T}_{0}\left(s-{s}_{0}\right)+{v}^{2}/2+{g}_{acc}\ast z$ into Equation (8) we can write

$\stackrel{\dot{}}{W}=\Sigma \left(1-{T}_{0}/{T}_{C}\right){\stackrel{\dot{}}{Q}}_{C}+\Sigma \stackrel{\dot{}}{m}\left[\left(h-{h}_{0}\right)-{T}_{0}\left(s-{s}_{0}\right)+{v}^{2}/2+{g}_{acc}\ast z\right]-{\stackrel{\dot{}}{E}}_{\text{destroyed}}$

When changes in kinetic and potential energies are negligible, the useful work per unit time is therefore given by:

$\stackrel{\dot{}}{W}=\Sigma \left(1-{T}_{0}/{T}_{C}\right){\stackrel{\dot{}}{Q}}_{C}+\Sigma \stackrel{\dot{}}{m}\left[\left(h-{h}_{0}\right)-{T}_{0}\left(s-{s}_{0}\right)\right]-{E}_{\text{destroyed}}$ (9)

where $\stackrel{\dot{}}{W}$ = Useful work per unit time or Exergy flow rate.

3.1. Exergy Destruction (E_{destroyed}) and Exergy Destruction Efficiency (ε_{D})

The exergy destruction in the system (gas power plant) is defined as the loss of available energy of the system. The exergy destruction efficiency is the ratio of exergy destroyed to the rate of exergy flow of fuel in the plant. That is,

${\epsilon}_{D}=100\ast {\stackrel{\dot{}}{E}}_{\text{destroyed}}/{\stackrel{\dot{}}{E}}_{F}$ (10)

From Equation (9) above, the useful work per unit time can be written as:

$\underset{\_}{\stackrel{\dot{}}{W}}={\underset{\_}{\stackrel{\dot{}}{W}}}_{rev}-{\stackrel{\dot{}}{E}}_{\text{destroyed}}$

where, ${\underset{\_}{\stackrel{\dot{}}{W}}}_{rev}$ is the reversible work per unit time and is given by:

${\underset{\_}{\stackrel{\dot{}}{W}}}_{rev}=\Sigma \left(1-{T}_{0}/{T}_{C}\right){\stackrel{\dot{}}{Q}}_{C}+\stackrel{\dot{}}{m}\left[\left(h-{h}_{0}\right)-{T}_{0}\left(s-{s}_{0}\right)\right]$ , (since ${\stackrel{\dot{}}{E}}_{\text{destroyed}}=0$ )

For the Compressor and the Gas turbine, the Exergy destroyed can be determined from the Guoy-Stodola relation of Equation (11) below

$\begin{array}{c}{\stackrel{\dot{}}{E}}_{\text{destroyed}}={T}_{0}{\stackrel{\dot{}}{S}}_{gen}\\ ={T}_{0}\left[{\stackrel{\dot{}}{m}}_{a}\left({s}_{1}-{s}_{2}\right)+{\stackrel{\dot{}}{Q}}_{surr}/{T}_{0}\right]\text{\hspace{0.17em}}\left(\text{for}\text{\hspace{0.17em}}\text{the}\text{\hspace{0.17em}}\text{compressor}\right)\\ ={T}_{0}\left[{\stackrel{\dot{}}{m}}_{g}\left({s}_{4}-{s}_{3}\right)+{\stackrel{\dot{}}{Q}}_{surr}/{T}_{0}\right]\text{\hspace{0.17em}}\left(\text{for}\text{\hspace{0.17em}}\text{the}\text{\hspace{0.17em}}\text{turbine}\right)\end{array}$ (11)

where ${\stackrel{\dot{}}{S}}_{gen}$ = Entropy generation.

${\stackrel{\dot{}}{Q}}_{surr}$ = Heat loss per unit time to the surrounding.

T_{0} = Reference temperature or dead state temperature.

3.2. Rational Exergy Efficiency, ε_{p}_{ }

Formulation

The rational exergy efficiency is defined [1] as the ratio of the desired exergy output (i.e. exergy recovered or actual useful exergy) to the exergy used (i.e. exergy supplied). It is given by;

$\begin{array}{c}{\epsilon}_{p}=\left(\text{exergy recovered}\right)/\left(\text{exergy supplied}\right)\\ =\left(\text{exergy supplied}-\text{exergy destroyed}\right)/\text{exergy supplied}\\ =\text{1}-\left(\text{exergy destroyed}/\text{exergy supplied}\right)p\end{array}$ (12a)

For an adiabatic turbine,

${\epsilon}_{turb}={\underset{\_}{\stackrel{\dot{}}{W}}}_{out}/{\underset{\_}{\stackrel{\dot{}}{W}}}_{rev,out}=\left({h}_{3}-{h}_{4}\right)/\left({\psi}_{3}-{\psi}_{4}\right)=1-{T}_{0}{\stackrel{\dot{}}{S}}_{gen}/\left({\psi}_{3}-{\psi}_{4}\right)$ (12b)

where, ${\psi}_{3}-{\psi}_{4}=\left({h}_{3}-{h}_{4}\right)-{T}_{0}\left({s}_{3}-{s}_{4}\right).$

For an adiabatic compressor,

${\epsilon}_{comp}={\underset{\_}{\stackrel{\dot{}}{W}}}_{rev,oin}/{\underset{\_}{\stackrel{\dot{}}{W}}}_{in}=\left({\psi}_{2}-{\psi}_{1}\right)/\left({h}_{2}-{h}_{1}\right)=1-{T}_{0}{\stackrel{\dot{}}{S}}_{gen}/\left({h}_{2}-{h}_{1}\right)$ (12c)

where

${\psi}_{2}-{\psi}_{1}=\left({h}_{2}-{h}_{1}\right)-{T}_{0}\left({s}_{2}-{s}_{1}\right)$

In Equation (9), If we let

${\stackrel{\dot{}}{E}}_{M}=\stackrel{\dot{}}{m}\left[\left(h-{h}_{0}\right)-{T}_{0}\left(s-{s}_{0}\right)\right]$ and ${\stackrel{\dot{}}{E}}_{T}=\left[1-{T}_{0}/{T}_{C}\right]{\stackrel{\dot{}}{Q}}_{C}={\stackrel{\dot{}}{Q}}_{C}-{T}_{0}{\stackrel{\dot{}}{Q}}_{C}/{T}_{C}$

Since, $h-{h}_{0}={c}_{p}\left(T-{T}_{0}\right)$ and $s-{s}_{0}={c}_{p}\mathrm{ln}\left(T/{T}_{0}\right)+R\mathrm{ln}\left({P}_{0}/P\right)$

Then,

${\stackrel{\dot{}}{E}}_{M}=\stackrel{\dot{}}{m}{c}_{p}\left[\left(T-{T}_{0}\right)-{T}_{0}\mathrm{ln}\left(T/{T}_{0}\right)-R\left({T}_{0}/{c}_{p}\right)\mathrm{ln}\left({P}_{0}/P\right)\right]$ (13)

where ${\stackrel{\dot{}}{E}}_{M}$ = Mechanical exergy stream of component.

For a reversible process involving a perfect gas with a unit mass,

${\stackrel{\dot{}}{Q}}_{C}={T}_{C}\left(s-{s}_{0}\right)$ and $s-{s}_{0}={c}_{p}\mathrm{ln}\left(T/{T}_{0}\right)+R\mathrm{ln}\left({P}_{0}/P\right)$

Therefore, ${\stackrel{\dot{}}{Q}}_{C}={T}_{C}\left[{c}_{p}\mathrm{ln}\left(T/{T}_{0}\right)+R\mathrm{ln}\left({P}_{0}/P\right)\right]$ and for a mass flowrate, ṁ, we can write,

${\stackrel{\dot{}}{E}}_{T}=\stackrel{\dot{}}{m}\left({T}_{C}-{T}_{0}\right)\left[{c}_{p}\mathrm{ln}\left({T}_{C}/{T}_{0}\right)+R\mathrm{ln}\left({P}_{0}/{P}_{C}\right)\right]$ (14)

where ${\stackrel{\dot{}}{E}}_{T}$ = Thermal exergy stream of the component.

3.3. Chemical Exergy of a Fuel Stream,
${\stackrel{\dot{}}{E}}_{F}$ _{ }

Chemical exergy of a fuel stream is defined as the maximum work that can be obtained from the fuel by taking it to chemical equilibrium with the reference environment at constant temperature and pressure. The determination of the chemical exergy of fuel is a particular case of the calculation of the chemical exergy of a stream and is of great interest in the analysis of industrial facilities because it measures the amount of energy released from the energy carrier (fuel) as the components in the energy carrier are brought into reaction with reference substances (composition of air at 25˚C and 1 atm pressure) present in the environment.

An approximate determination of the specific chemical exergy of industrial fuels can be easily carried out through empirical coefficients f_{l} and f_{h} [9] which relate it to the lower or higher heating values, i.e.

${\stackrel{\dot{}}{E}}_{F}={f}_{l}\ast LHV={f}_{h}\ast HHV$

where ${\stackrel{\dot{}}{E}}_{F}$ denotes the chemical exergy of fuel.

In this study, we assume the relationship [4] [9] to be that of Equation (15), i.e.

${\stackrel{\dot{}}{E}}_{F}=\left(1.0308+{\stackrel{\dot{}}{m}}_{F}\right)\ast LHV$ (15)

Taking note of the various components defined by Equation (9), the general exergy balance equation can be written as:

${\stackrel{\dot{}}{E}}_{F}+{\stackrel{\dot{}}{E}}_{T}+{\stackrel{\dot{}}{E}}_{M}-{\stackrel{\dot{}}{E}}_{\text{destroyed}}=\stackrel{\dot{}}{W}$ (16)

where $\stackrel{\dot{}}{W}$ denotes the Exergy flow rate of the system, and

${\stackrel{\dot{}}{E}}_{F}$ = Chemical exergy of fuel.

${\stackrel{\dot{}}{E}}_{T}$ = Thermal exergy stream of the component under consideration.

${\stackrel{\dot{}}{E}}_{M}$ = Mechanical exergy stream of the component under consideration.

3.4. Combustion Efficiency, η_{cc}_{ }

The combustion chamber provides the heat for the working substance (air and fuel) in a gas turbine power plant. In practice the characteristics of a gas power plant are primarily determined by the reliability, starting properties, long service life, and the economy of operation of the combustion chamber [10] . The combustion efficiency is obtained from the relation:

Heat supplied by fuel = Heat taken by burning gas

i.e. ${\stackrel{\dot{}}{m}}_{F}\ast LHV\ast {\eta}_{cc}={\stackrel{\dot{}}{m}}_{g}\ast {c}_{P}\ast \left({T}_{3}-{T}_{2}\right)$ (17)

where η_{cc} is the combustion efficiency.

3.5. Heat Rate (HR) of the Gas Power Plant

The Net Plant Heat rate is defined as the amount of fuel energy input required to generate a kWh of electricity. Mathematically,

Heat rate (kJ/kWh) = Input Energy (kJ/h)/Output Power (kW)

The heat rate is simply the inverse of the energy efficiency. Thus, If the plant efficiency is increased, the heat rate is lowered, and the better the plant is running because it is consuming less fuel. The plant heat rate is a measure of the combined performance of the gas turbine cycle and any other associated auxiliaries. When calculating the plant heat rate, the energy input to the system is the chemical energy in the fuel. Thus, Chemical energy of fuel = Total fuel used (kg/h) × LHV (kJ/kg), we can therefore write,

Net plant heat rate (kJ/kWh)

= (Chemical energy of fuel, kJ/h)/(Net Output power, kW) (18)

3.6. Relationship between Exergy Efficiency (ε_{p}) and Heat Rate (HR) of a Gas Power Plant

Equation (12a) defines the exergy efficiency, ε_{p}, to be

$\begin{array}{c}{\epsilon}_{p}=\text{1}-\left(\text{exergy destroyed}\right)/\left(\text{exergy supplied}\right)\\ =\text{1}-{E}_{\text{destroyed}}/\left(\text{Available energy in Fuel}\right)\\ =\text{1}-{E}_{\text{destroyed}}/{E}_{F}\end{array}$ (19)

Similarly, Equation (18) defines the heat rate, HR, to be

$\begin{array}{c}\text{HR}=\text{Chemical energy of fuel}/\text{Net output power}\\ =\text{Chemical energy of fuel}/{P}_{\text{out}}\end{array}$ (20)

where, P_{out} is the net output power from the plant in kW.

Equation (20) gives

$\text{Chemical Energy of fuel}=\text{HR}\ast {P}_{\text{out}}=\text{Input Energy}$ (21)

The exergy destroyed in the plant, E_{destroyed}, is the sum of exergy destroyed in the air compressor (E_{DAC}), combustion chamber (E_{Dcc}) and the gas turbine (E_{DGT}). Thus,

${E}_{\text{destroyed}}={E}_{\text{DAC}}+{E}_{\text{Dcc}}+{E}_{\text{DGT}}$ (22)

From the operational data in Tables 1-3, Equation (22) yields

34.45 MW = 1.80 MW + 32.08 MW + 0.57 MW

Thus,

${E}_{\text{destroyed}}=1.08\ast {E}_{\text{Dcc}}$ (23)

i.e. the exergy destruction in the plant is 1.08 times the exergy destruction in the combustion chamber.

But the exergy destroyed in the combustion chamber,

${E}_{\text{Dcc}}=\text{Chemical energy of fuel}\ast {\eta}_{cc}$ (24)

where η_{cc} is the thermal efficiency of the combustion chamber.

Also, the exergy supplied to the plant,

${E}_{F}=\text{Exergy in the combustion chamber}={\stackrel{\dot{}}{m}}_{F}\ast 3600\ast LHV$ (25)

where ${\stackrel{\dot{}}{m}}_{F}$ , is the mass flow rate of the fuel in kg/s.

Substituting Equations (21), (23), (24) and (25) into Equation (19) yields

${\epsilon}_{p}=1-\left[1.08\ast \left(HR\right)\ast {P}_{\text{out}}\ast {\eta}_{cc}\right]/\left[{\stackrel{\dot{}}{m}}_{F}\ast 3600\ast \left(LHV\right)\right]$ (26)

where ${\epsilon}_{p}$ is the exergy efficiency of the plant.

Equation (26) is the derived relationship between the exergy efficiency and the heat rate of the gas power plant. It shows that the exergy efficiency of a power plant can be estimated for a given heat rate provided we know the output power, mass flow rate of the fuel and the thermal efficiency of the combustion chamber.

3.7. Assumed Constants in the Analysis

In this study, the following thermodynamic constants are used in the calculations:

Specific gas constant, R = 0.287 kJ/kg K.

Specific heat capacity at constant pressure for air, C_{pa} = 1.005 kJ/kg K.

Specific heat capacity at constant pressure for exhaust gas, c_{pg} = 1.11 kJ/kg K.

Convective heat transfer coefficient, hcoeff = 50 W/m^{2}K.

LHV of fuel (methane) = 50,000 kJ/kg.

3.8. Reference Conditions

The reference conditions assumed for the power plant in the analysis are:

T_{0} = 298.150 K (for cold rated condition).

T_{0} = 310.150 K (for hot rated condition).

P_{0} = 1.013 bars.

4. Exergy Analysis of a 30 MW AES Gas Power Plant

The following assumptions are made in the analysis:

1) The kinetic and potential exergies are negligible.

2) The system (Gas turbine plant) is real, i.e. non-isentropic processes are considered for the analysis.

3) Heat losses through conduction and radiation are considered negligible.

4) The processes in the system are steady flow processes.

The exergy balance equation for each of the major components of the AES Gas Turbine plant can be derived from the general exergy balance equation given in Equation (16).

Using the states as represented in the T-S diagram for the plant (given in Figure 2), the exergy balance equation for each of the gas power plant components is as follow:

4.1. Air Compressor

${E}_{T}+{E}_{M}-{\stackrel{\dot{}}{E}}_{\text{destroyed}}={\stackrel{\dot{}}{W}}_{AC}$ _{ }

4.2. Combustion Chamber

$\left({E}_{F}+{E}_{T}+{E}_{M}\right)-{\stackrel{\dot{}}{E}}_{\text{destroyed}}={\stackrel{\dot{}}{Q}}_{surr}$

where ${\stackrel{\dot{}}{Q}}_{surr}$ denotes the heat transfer rate between the combustion chamber and the environment.

4.3. Gas Turbine

${E}_{T}+{E}_{M}-{\stackrel{\dot{}}{E}}_{\text{destroyed}}={\stackrel{\dot{}}{W}}_{GT}$

where

${\stackrel{\dot{}}{W}}_{AC}$ = Exergy flowrate of air compressor.

${\stackrel{\dot{}}{W}}_{GT}$ = Exergy flowrate of gas turbine.

E_{F} = Chemical exergy of fuel.

E_{T} = Thermal exergy stream of the component in consideration.

E_{M} = Mechanical exergy stream of the component in consideration.

${\stackrel{\dot{}}{E}}_{\text{destroyed}}$ = Exergy destruction rate.

The above terms are evaluated from the relations of Equations (11), (13), (14) and (15).

4.4. The Following Entropy Changes Should Also Be Noted

${s}_{2}-{s}_{1}={c}_{p}\mathrm{ln}\left({T}_{2}/{T}_{1}\right)+R\mathrm{ln}\left({P}_{1}/{P}_{2}\right)$ for compression process (27)

${s}_{4}-{s}_{3}={c}_{p}\mathrm{ln}\left({T}_{4}/{T}_{3}\right)+R\mathrm{ln}\left({P}_{3}/{P}_{4}\right)$ for expansion process (28)

${s}_{3}-{s}_{2}={c}_{p}\mathrm{ln}\left({T}_{3}/{T}_{2}\right)$ for combustion process (29)

5. Results and Discussion

5.1. Exergy Analyses of the 30 MW Gas Power Plants

Table 4 shows the results of the exergy analysis for the gas power plant A at 90% maximum continuous rating (MCR). Similar results were also obtained for the gas power plants B and C. The exergy flow rate of the net power output for plant A is 57.78 MW compared with 60.43 MW for plant B and 67.07 MW for plant C. In the case of the total exergy destruction, plant A is found to be 34.40 MW while the corresponding exergy destructions in plants B and C are 46.04 MW and 35.58 MW respectively. Thus, the loss of available energy of the system is maximum in plant B.

Table 4. Exergy flow rate, exergy destruction, exergy destruction efficiency and rational exergy efficiency for 30 MW gas power plant A at 90% MCR.

The exergy efficiency of the air compressor in plant A is 90.86% compared with the corresponding values of 92.42% and 93.26% in plants B and C respectively. The turbine section in plant A has an exergy efficiency of 99.39% compared with 99.30% and 99.40% in plants B and C respectively. Thus, from a practical standpoint, the three plants (A, B and C) have turbines with identical performance.

The combustion chamber in plant A has the exergy destruction efficiency of 19.04% while the corresponding values for plants B and C are 25.06% and 18.87% respectively.

The rational exergy efficiency of the overall 30MW gas power plant is 35.44% in plant A and the corresponding values in plants B and C are 34.92% and 38.32% respectively. Thus, the actual useful energy is maximum in plant C.

5.2. Energy Efficiencies of the Major Components of Gas Power Plants A, B and C

Table 5 shows the results of the computed energy efficiencies of the major components of the three gas power plants. The air compressor of gas power plant C has the highest isentropic efficiency of 85.10% while the combustion chamber of the gas power plant A has the highest energy efficiency of 58.99%. The isentropic efficiencies of the turbines in gas power plants B and C are identical at 90.70%.

5.3. Exergy and Energy Efficiencies of the Combustion Chambers in 30 MW Gas Power Plants

When compared to other major components of the gas power plant, the exergy efficiency of the combustion chamber was found to significantly increase with the gas turbine inlet temperature as shown in Figure 4 for plant A.

This makes the combustion chamber the choice component to be optimized in the overall performance of the gas power plant. The correlation between the exergy and energy efficiencies of the combustion chamber in 30 MW gas power plants in the study is shown in Figure 5 to follow the relation:

${\epsilon}_{cc}=9.56+1.22\ast {\eta}_{cc}$

with a correlation coefficient of 0.966.

Table 5. Energy efficiencies of the major components of the three gas power plants.

Figure 4. Change in overall plant rational exergetic efficiency with turbine inlet temperature for AES Gas Power Plant at 90% MCR.

Figure 5. Correlation between the combustion chamber exergy and energy efficiencies in a 30 MW gas power plant.

5.4. Rational Exergy Efficiency (ε_{p}) and Heat Rate (HR) of the 30 MW Gas Power Plants

The results of the operational data of heat rate, actual output power, fuel mass flow rate and computed rational exergy efficiency of each gas power plant are compared with the predicted rational exergy efficiency according to Equation (26) in Table 6. The table shows that from consideration of the operational heat rate of the plants, plant C is the most fuel efficient followed by plant A, while plant B is the least efficient. In the case of the prediction, we have assumed the output power to be 30 MW while the heat rate and the fuel mass flow rate have been assumed to be the average operational values for the three turbines of 14,100 kJ/kWh and 2.38 kg/s respectively. The combustion chamber energy efficiencies in Table 5 have been used in the prediction. The gas power plant B can be seen to exhibit the maximum deviation in exergy efficiency of about 21.5% from the calculated operational value of 34.9% while the plants A and C exhibited deviations of about 4.7% and 0.4% respectively from the computed operational values of 35.4% and 38.3% In general it can be deduced that Equation (26) is a reasonable relationship between the rational exergy efficiency and the heat rate of a gas power plant.

Also, from Equation (26), the rational exergy efficiency can be seen to increase with increasing mass flow rate of the fuel at a given heat rate and combustion chamber thermal efficiency. The maximum theoretical mass flow rate of the fuel,
${\left({\stackrel{\dot{}}{m}}_{F}\right)}_{\mathrm{max}}$ , will correspond to when the rational exergy efficiency approaches the Carnot efficiency, η_{carnot}, of the gas power plant. The Carnot efficiency of a 30 MW gas power plant can be computed from the relation,

${\eta}_{\text{carnot}}=\left({T}_{3av}-{T}_{0}\right)/{T}_{3av}$

where T_{3av} = 1473.13 K is the average value of the operational inlet temperature to the turbine for the three gas power plants. T_{0} is the reference temperature. Thus, η_{carnot} can be computed to be 0.7976% or 79.76%. Using this value in Equation (26) for a 30 MW gas power plant, with η_{cc} = 0.59, HR = 14,100 kJ/kwh, gives the theoretical maximum mass flow rate of fuel as
${\left({\stackrel{\dot{}}{m}}_{F}\right)}_{\mathrm{max}}$ = 7.40 kg/s. The average operational value of
${\stackrel{\dot{}}{m}}_{F}$ = 2.38 kg/s shows that about one-third of the theoretical maximum mass flow rate of fuel is used in practice. Figure 6 shows the non-linear regression relation between the rational exergy efficiency and the mass flow rate of fuel to be,

${\epsilon}_{p}=95.80-433.75/\left(1+2.18\ast {\stackrel{\dot{}}{m}}_{F}\right)$

with a correlation coefficient of 1.00.

Figure 7 also shows that in the 30 MW gas power plants in the study, the exergy efficiency of the combustion chamber may be expressed as a function of the rational exergy efficiency of the plant with the following relation:

${\epsilon}_{cc}=-4523+250\ast {\epsilon}_{p}-3.4\ast {\epsilon}_{p}^{2}$

with a correlation coefficient of 1.0.

Figure 6. Nonlinear regression of Exergy efficiency (ε_{p}) of a 30 MW Gas Power Plant as a function of Mass flow rate of fuel (
${\stackrel{\dot{}}{m}}_{F}$ ) for HR = 14,100 kJ/kWh and η_{cc} = 0.59.

Table 6. Comparison and validation of the predicted data with operational data for the exergy efficiency of 30 MW gas power plant.

Figure 7. The combustion chamber exergy efficiency as a function of the rational exergy efficiency of a 30 MW gas power plant.

6. Conclusions

On the basis of the analyses of the thermodynamic performance of the major components of three operational gas power plants in Lagos Nigeria, each with a rated capacity of 30 MW but from different Original Equipment Manufacturers (A, B and C), the heat rate shows that plant C is the most fuel efficient of the three plants. The rational exergy efficiency is found to be a useful parameter in identifying and quantifying the possible areas of reduction in thermodynamic losses and improvement in efficiencies of major components in a gas power plant. The analysis has demonstrated that the rational exergy efficiency of a gas power plant (ε_{p}) for a given power output (P_{out}) is a function of the heat rate, (HR), the mass flow rate of the fuel (
${\stackrel{\dot{}}{m}}_{F}$ ) and the thermal energy efficiency of the combustion chamber (η_{cc}). A relationship between the rational exergy efficiency and the heat rate of the gas power plant in this study has been shown to be:

${\epsilon}_{p}=1-\left[1.08\ast \left(HR\right)\ast {P}_{\text{out}}\ast {\eta}_{cc}\right]/\left[{\stackrel{\dot{}}{m}}_{F}\ast 3600\ast \left(LHV\right)\right]$

This relationship has been validated to explain the operational rational exergy efficiency of each of the three gas power plants (A, B and C) in the study.

The exergy efficiency of the combustion chamber which provides the maximum exergy destruction in gas power plants is shown to exhibit the following correlations with its thermal energy efficiency and the plant rational exergy for the 30 MW capacity gas power plants.

${\epsilon}_{cc}=9.56+1.22\ast {\eta}_{cc}$

with a correlation coefficient of 0.966.

And

${\epsilon}_{cc}=-4523+250\ast {\epsilon}_{p}-3.4\ast {\epsilon}_{p}^{2}$

with a correlation coefficient of 1.0.

The theoretical maximum mass flow rate of fuel in a 30 MW gas power plant, (ṁ_{F})_{max} = 7.40 kg/s, has been shown to correspond to when the rational exergy efficiency approaches the Carnot efficiency of the plant. However, practical operational mass flow rate of the fuel has been shown to correspond to about one-third of the theoretical maximum mass flow rate of fuel.

The novelty in the study is the demonstration that the exergy efficiency of a 30 MW gas power plant can be estimated for a given heat rate provided the output power, mass flow rate of the fuel and the thermal efficiency of the combustion chamber are known.

The practical implication is that from an operational and component selection viewpoint in the specifications of a gas power plant, knowledge of the Heat Rate which is usually provided by the OEM is adequate to make a reasonable inference on the performance of some critical components of the plant.

Acknowledgements

The authors would like to acknowledge with thanks the support given by the management of AES Nigeria Barge Operations Ltd. to the authors in the provision of the operational data used in this study.

Nomenclature

Greek Alphabet

ε: Exergy efficiency

ε_{D}: Exergy destruction efficiency

η_{AC}: Isentropic efficiency of air compressor

η_{Carnot}: Carnot Efficiency

η_{CC}: Combustion efficiency

η_{GT}: Isentropic efficiency of gas turbine

ψ: Exergy content

Lower case letters

c_{P}: Specific heat capacity at constant pressure (kJ/kgK)

gacc: Acceleration due to gravity (m∙s^{−2})

h: Specific enthalpy (kJ/kg)

hcoeff: Convective heat transfer coefficient(W/m^{2}∙K)

k: Ratio of specific heat capacities

$\stackrel{\dot{}}{m}$ : Mass flow rate of working fluid [air/fuel] (kg/s)

${\stackrel{\dot{}}{m}}_{a}$ : Mass flow rate of air (kg/s)

${\stackrel{\dot{}}{m}}_{f}$ : Mass flow rate of fuel(kg/s)

${\stackrel{\dot{}}{m}}_{e}$ : Mass flow rate of exhaust gas (kg/s)

s: Specific entropy (J/kg K)

u: Specific internal energy (J/kg)

v: Velocity (m∙s^{−1})

z: Height (m)

Upper case letters

A: Area (m^{2})

CTD: Compressor discharge temperature (˚K)

CTI: Compressor inlet temperature (˚K)

E: Exergy

Ė_{destroyed}: Exergy destruction rate

E_{F}: Chemical exergy of fuel

E_{M}: Mechanical exergy stream of component

E_{T}: Thermal exergy stream of component

HHV: Higher heating value (kJ/kg)

HR: Heat Rate (MJ/kWh)

LHV: Lower heating value (kJ/kg)

MCR: Maximum Continuous Rating

P: Pressure (bar)

PA: Ambient pressure (bar)

P_{c}: Pressure at location c (bar)

PCD: Compressor discharge pressure (bar)

P_{F}: Fuel pressure (bar)

P_{1}: Pressure of air before compression (bar)

P_{2}: Discharged pressure of air after compression (bar)

P_{3}: Pressure of gas at the inlet of turbine (bar)

P_{4}: Pressure of gas after expansion (bar)

Q: Heat transfer energy (J)

Q_{C}: Heat transfer through the boundary at temperature Tc at location c (J)

${\stackrel{\dot{}}{Q}}_{C}$ : Heat transfer per unit mass through the boundary at temperature Tc at location c (W)

${\stackrel{\dot{}}{Q}}_{Surr}$ : Heat loss per unit mass to the surrounding (W)

R: Specific gas constant (kJ/kg K)

S_{gen}: Entropy generation (kJ/kg K)

SLT: Second Law of Thermodynamics

T: Temperature (˚K)

T_{C}: Temperature at location c (˚K)

T_{F}: Temperature of fuel (˚K)

TIT: Turbine Inlet Temperature (˚K)

TP: Total Gas Power Plant

T_{0}: Reference temperature (˚K)

T_{1}: Inlet temperature of air to the compressor (˚K)

T_{2}: Exit temperature of air after compression (˚K)

T_{2S}: Isentropic temperature of air at compressor exit (˚K)

T_{3}: Inlet temperature to the turbine after combustion (˚K)

T_{4}: Exit temperature of gas after expansion (˚K)

T_{4S}: Isentropic temperature of exhaust gas at turbine exit (˚K)

U: Internal energy (J)

V: Volume (m^{3})

W: Boundary work through the system (J)

$\stackrel{\dot{}}{W}$ : Exergy flow rate or Useful work per unit time of the system (W)

${\stackrel{\dot{}}{W}}_{net}$ : Net Exergy flow rate of the unit or system (W)

${\stackrel{\dot{}}{W}}_{rev}$ : reversible work per unit time (W)

Subscripts

A: Air

B: Boundary

AC: Air Compressor

c: Localized point

C: Compressor

CC: Combustion Chamber

coeff: Coefficient

Comb: Combustion

CV: Control volume

D: Destruction

exh: Exhaust

F: Fuel

g: Exhaust gas

gen: generation

GT: Gas turbine

i: Initial state

j: Final state

M: Mechanical

o: Out

rev: Reversible

surr: Surrounding

T: Thermal

0: Reference state or dead state

Superscripts

T: Thermal

M: Mechanical

1: Air compressor inlet state

2: Air compressor exit state

3: Combustion chamber exit state

4: Gas turbine exit state

F: Fuel

Conflicts of Interest

The authors declare no conflicts of interest regarding the publication of this paper.

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