Development of an innovative cogeneration system for fresh water and power production by renewable energy using thermal energy storage system

Sustainable Energy Technologies and Assessments 37 (2020) 100572

Contents lists available at ScienceDirect

Sustainable Energy Technologies and Assessments journal homepage: www.elsevier.com/locate/seta

Development of an innovative cogeneration system for fresh water and power production by renewable energy using thermal energy storage system B. Ghorbania, R. Shirmohammadib, M. Mehrpooyab, a b

T

⁎

Faculty of Engineering Modern Technologies, Amol University of Special Modern Technologies, Amol, Iran Department of Renewable Energy and Environment, Faculty of New Sciences & Technologies, University of Tehran, Iran

A R T I C LE I N FO

A B S T R A C T

Keywords: Solar collectors Phase change material Steam power plant Multi-staged thermal water Exergy analysis Sensitivity analysis

In this paper, solar dish collectors incorporated with phase change material storage are used for providing the required thermal energy of a steam power plant with a net production capacity of 1063 MW. The storage of phase-change material is employed during the night and in the absence of solar thermal sources. In order to prevent heat losses in the condenser, a large part of the dissipated heat is given to a multi-effect desalination system. The desalination system generates 8321 kg/s of fresh water by utilizing 2571 MW of waste heat from the steam power plant. This hybrid system has a total electrical efficiency of 28.84%, and total thermal efficiency of 97.18%. Exergy analysis is used to examine the integrated structure by means of the second law of thermodynamic. The exergy efficiency of the whole integrated structure is 52.23%, and the highest share of exergy destruction among equipment is related to heat exchangers and collectors with 46.83% and 40.93%, respectively. Hysys, Transys, and Matlab software are used in order to simulate the hybrid system by means of the weather input data of the case study, i.e. the city of Bushehr. Sensitivity analysis of the vital indicators of the system is conducted, and suitable solutions for improving the model and determining the amount of decision making parameters are made.

Introduction The Iran solar resource is considered among the best in the world. The country is blessed with abundant space and plenty of solar hours. This issue leads to attracting the local and international investment for solar power generation. Small-scale solar collection using photovoltaic panels and solar water heaters are becoming more popular, and largescale grid-connected solar power plants have a growing tendency in Iran [1]. The two major problems of water and energy crisis threaten the day-to-day life of humans [2]. In the past, the use of fossil fuels and surface water resources has solved these two crises. Today, with the reduction of surface water resources and the need for the use of water with the ability to remove inappropriate material to have high quality, which itself requires the use of an energy source, researchers are pushing the replacement of renewable energies for use in sweetening the water [3]. Water is considered one of the most important human needs [4]. Although three-quarters of the earth's surface is covered with water, only 3% of the water is sweet, and the rest is seawater and ocean water. Of this 3%, 77% is in the form of polar ice, 22% in groundwater and only 1% in rivers and lakes. Among the various methods of producing freshwater, desalination systems are more common and more

⁎

efficient [5,6]. In this realm, a variety of hybrid desalination systems have been developed. Additionally, using of concentrating photovoltaic-thermal hybrid systems have recently attracted attention of scholars [7]. Ariyanfar et al. [8] analyzed a solar organic Rankine cycle that simultaneously generates heat and power using energy, exergy, economic and environmental analyses. In this study, solar energy and natural gas were used to provide primary energy. Ghorbani et al. [9] developed an integrated hybrid flat-plate collector system to supply the required energy, and Kalina cycle for power generation cycle in conjuction with multi-effect desalination process . The system has the capability of producing the power of 1869 kW, heating of 65194 kW and fresh water production of 83.22. They concluded that the developed system has total thermal and exergy efficiency of 44.64% and 90.04%, respectively. Shakib et al. [10] developed a multi-stage desalination system with combined cycle equipped with heat recovery boilers. After simulating and analyzing of the system, the effect of functional parameters of the system such as functional pressure levels, the temperature of the input gas into the boiler, the temperature of the pinch for pressure levels, etc., on the total exergy efficiency of the system were investigated. As one of the results, the power of the steam turbine increases with a high operating pressure up to a maximum

Corresponding author at: Renewable Energies and Environment Department, Faculty of New Sciences and Technologies, University of Tehran, Tehran, Iran. E-mail address: [email protected] (M. Mehrpooya).

https://doi.org/10.1016/j.seta.2019.100572 Received 1 April 2019; Received in revised form 19 September 2019; Accepted 7 November 2019 2213-1388/ © 2019 Published by Elsevier Ltd.

Sustainable Energy Technologies and Assessments 37 (2020) 100572

B. Ghorbani, et al.

Nomenclature

Aa Ac Aw Qs Is Qr Qu Ql Qlk Qlc Qlr Nul Tw Ta Grl g L hc

K Kt Gon Gsc c H0 Hd Is Id It ms hs Llog D CP Ra Eẋ ṁ T0 si ex h0 s0 ṅi

xi ei0

Surface area of the concentrator (m2) Surface area of the receiver aperture (m2) Cavity internal area of receiver (m2) Power reached on the surface of the dish (W) Beam solar radiation reached to concentrator surface (W/ m2) Power reached to the receiver (W) Useful thermal power reached to the receiver (W) Power lost in the receiver (W) Power lost from receiver through conduction (W) Power lost from receiver through convection (W) Power lost from receiver through radiation (W) Nusselt number (–) Receiver temperature (°C) Ambient Temperature (°C) Grash of number Gravitational acceleration (9.806 m/s2) Diameter (m) Convection heat transfer coefficient between the absorber and air and ambient air, W/m2K Thermal conductivity of the ambient air, W/m K Clearness index of a day Extraterrestrial radiation incident Solar constant (1367 W/m2) Geometrical concentration ratio (–) Extraterrestrial solar radiation on a horizontal surface Daily diffuse solar radiation Hourly global solar radiation on the horizontal surface Hourly diffuse solar radiation on the horizontal surface Hourly global solar radiation on the tilted surface Heating steam mass flow rate Specific enthalpy of the heating steam Local geographical longitude Distillated mass flow rate (kg/s) Specific heat capacity Entrainment ratio of the steam ejector Exergy rate (kW) Mass flow rate (kg/s) Temperature of the dead state (K) specific entropy (kJ/kg.K) Specific exergy (kJ/kg) Specific enthalpy at reference state (kJ/kg) Specific enthalpy at reference state (kJ/kg.K) Mole rate of the ith stream (mole/kg)

in out Q̇ Ẇ h ηex

Mole fraction of the j th component in the stream Standard chemical exergy of the component in the stream (kJ/mole) Input Output Rate of heat transfer (kW) Rate of shaft work (kW) Specific enthalpy Exergy Efficiency

Greek Letters

γi ρ λ τ α γ η φ1 β v δ ∅ ωs εeff εc σ ω

Activity factor Reflectance Land factor of un-shading Transmittance Absorptance Intercept factor Efficiency (%) Tilt angle of cavity (Radian) Coefficient of thermal expansion (1/°C) Kinematic viscosity (m2/s) Declination Latitude Sunset hour angle Effective infrared emittance of cavity Cavity surface emittance Stefan–Boltzmann constant (5.67 × 10−8 W/m2 K4) Hour angle

Subscripts and superscripts

ex ph ch o r c

Exergy Physical Chemical Optical Receiver Collector

Abbreviation MED SDC IS PCM

Multi effect desalination Solar dish collector Integrated structure Phase change material

efficiency is increased by 43.91%. Maleki et al. [15] developed a coproduction system for water and power using a photoluminescence system, wind turbine, fuel cell, and desalination system. They improved the IS using economic analysis and system optimization. In order to provide hydrogen production in this IS, the electrolyzer was used for the production of fresh water from the RO desalination system. Ahmadi et al. developed many new methods of power generation [16,17]. They developed an integrated cogeneration structure with the molten carbonate fuel cell and CO2 Brayton cycle. Multi-objective optimization was used to evaluate the newly developed structure [18]. Due to the water and energy crisis, improving the efficiency of thermal systems and heat recycling along with the use of the water desalination process has attracted the attention of many researchers in recent years. Javadi and et al. modified the structure of the Bandar Abbas steam power plant. They used solar collectors to supply input heat, organic Rankine cycles for auxiliary power generation cycles, and thermal desalination cycle to replace the condenser [19]. Piadehrouhi et al. [20] developed a

value and then it decreases. Then, using a single-objective genetic algorithm and a two-objective, optimization energy and economic structure of the integrated structure (IS) were conducted [11]. The solar energy ratio used to provide the heat supply of the entire IS is equal to 24.2% [6]. Ashouri et al. [12] developed a Kalina cycle with a solar thermal heat source. A storage tank is used to save energy. The proportion of solar energy used to supply heat to the entire IS in this paper is 69%. In the IS, the overall electrical exergy efficiency is 5.24%, and the total thermal exergy efficiency is 62%. In an integrated solar combined cycle plant using parabolic collectors is introduced and analyzed [13]. The results indicate that in the proposed solar power plant average efficiency is 60.9%. Ahmadi et al. [14] used solar collectors to heat the Isfahan steam power plant, located in Isfahan province, in Iran. In order to pre-heating the input water which is entered into the recovery boiler, seven different scenarios were used. In the scenario of replacing the solar collector instead of all high-pressure boilers, the energy efficiency is increased by 45% and the exergy 2

Sustainable Energy Technologies and Assessments 37 (2020) 100572

B. Ghorbani, et al.

store refrigeration using the Hysys, Transys, and Matlab software In order to evaluate the system, the energy and exergy analyses were employed and the overall thermal and total exergy efficiencies of the system were obtained with the amount of 60.51% and 50.84%. One of the major problems of power plants in the world is carbon dioxide emission from the heat source due to the consumption of fossil fuels and natural gas. A significant portion of the heat in the condenser of the power plant is also wasted, or requires large water sources for cooling. Extensive studies have been carried out to replace high temperature solar collectors to supply input heat to the plant to reduce CO2 emissions and natural gas consumption. Extensive studies have also been carried out to utilize the heat lost in the condenser for water desalination. Supplying heat for integrated freshwater and power systems during the night is one case that has not been studied. In this paper, the process of thermal desalination and solar collectors are dynamically used in steam power plants along with the thermal phase change system in a specific climatic condition. An integrated power generation cycle has been developed with the aid of the solar collector as a heat supplier. The heat should be cooled at high temperature causing many environmental problems, thus, it is used to sweeten the seawater using a multi-effect desalination method.

hybrid power production system comprising molten carbonate fuel cell, solar parabolic dish, Oxy-fuel and Rankine power generation cycles equipped with CCS unit and liquefaction process. The system was analyzed through the exergy approach and the overall exergy efficiency of the system was attained 63.19%. Khoshgoftar Manesh et al. [21] conducted a multi-objective thermoeconomic analysis of a steam power plant with MSF sweating water. The 3000 MW nuclear power plant was used to supply heat. They used to pinch and exergy analyses to modify the network heat exchanger. Peng et al. [22] developed two ISs of the steam power plant driven by solar. The exergy analysis of the two ISs disclosed that the share of exergy destruction of solar collectors is 62.81% and 64.84%, respectively. Blumberg et al. [23] conducted the exergoeconomic assessment for two cases of power generation in power plant. The F-Class has an electric efficiency of 58.7% and H-Class has an electrical efficiency of 60%. The exergy analysis of these two structures exposed that, the production of F-Class power is 56% and for the steam cycle, and the production of H-Class power is 58.3% according to the exergy efficiency of the steam cycle. Akbari et al. [24] developed a new hybrid system, utilizing geothermal energy as a heat source, and contains a Kalina cycle, a LiBr/H2O heat transformer, and a water desalination system for generating power and pure water. Ansari et al. [25] developed an integrated power plant for the production of water with a MED system. The IS has a capacity of 24,000 tons per day for freshwater production, and the GOR is 8.81 for this 7-stage desalination system. Meratizaman et al. [26] presented several integrated power and heat generation systems for heavy fuel oil gasification for use in fuel cell and desalination system. They used sensitivity, exergy, and economic analyses to evaluate the ISs [27]. Ghorbani et al. [28]developed a natural gas fired power plant integrated with two regenerative boilers, in which parabolic solar dish collectors a replaced with the one of the boilers. The thermal energy was stored by PCM in a storage tank. They concluded that presence of an auxiliary boiler to deliver constant load for the whole day is vital. They also concluded that the new configuration declined the energy efficiency slightly, yet the exergy efficiency of the power plant increased. Ghorbani et al. [29] investigated an integrated structure includes photovoltaic-thermal collector, ejector refrigeration cycle and phase change material storage energy system to generate and

Process description Fig. 1 demonstrates an integrated power and heat generation from a solar power plant. The coding is developed in Matlab software to simulate the solar collectors, and Hysys simulator and Matlab programming language are employed for simulating the system of the steam power plant and desalination system. The desired climatic information in this article is related to city of Bushehr located in the south of Iran, which is extracted by the Transys software. Fig. 2 illustrates the IS of power and fresh water production equipped with the solar dish collector. This IS can produce 1063 MW of net power and 8321 kg/s of fresh water. Table 1 depicts the mole fraction of each stream in the IS. This table presents that the oil used in the oil cycle has a molar ratio of 0.2462 for BiPhenyl and 0.7528 for diPH-Ether. Table 2 depicts the temperature, pressure, and mass flow rates of the IS. Table 3 depicts the

Fig. 1. The block diagram of the IS. 3

Sustainable Energy Technologies and Assessments 37 (2020) 100572

B. Ghorbani, et al.

Fig. 2. The process flow diagram of the IS.

h (φ1) = 1.1677 − 1.0762 sin(φ10.8324 )

Table 1 The molar ratio of some streams in the IS. Stream

Water

Sodium Chloride

BiPhenyl

diPH-Ether

Oil 1 100 130 201, 208 209 213 214, 220 221 (Brine) 227 (Desalinated Water) 228 (Sea Water)

0 1 1 1 0.9768 0.9495 1 0.9292 1 0.9610

0 0 0 0 0.0232 0.0505 0 0.0708 0 0.0390

0.2462 0 0 0 0 0 0 0 0 0

0.7528 0 0 0 0 0 0 0 0 0

(5)

Nul = 0.106Grl1/3 (Tw / Ta)0.18 (4.256Ac / Aw ) sh (φ1) Nusselt number based on length L hc = Nul K / L

(8)

εeff = 1/[1 + (1/εc − 1) Ac /Aw ] Effective infrared emittance of the cavity (9)

A c = Aa / c

Entrance aperture area of the receiver

(11)

Ql = Qlk + Qlc + Qlr

Heat losses from the receiver to the surroundings (12)

Qu = Qr − Ql Absorbing part is the main component of the solar dish collector system. The action of absorbing solar radiation and transferring heat to the fluid is done by this section. The solar collector must have good heat transfer properties and thermal conductivity as well as the high coefficient of absorption [30,31]. It must be stable against high temperatures and have low-emission coefficient. Moreover, it must be resistant to internal and external corrosion. The collector's efficiency depends entirely on the condition and material which are used to make it. Solar parabolic plates are considered to be on two axes of the sun to reach the required temperature in the absorption section, which is 1230 K. The power of each dish can be obtained from the following relationships. The the total amount of energy lost from the absorber of the dish can be obtained by means of following equation, in which Qlk is equal to the heat lost during conduction in the absorber. Qlc and Qlr are equal to the conduction and radiation heat lost at the absorber aperture.

Solar energy incident on the dish concentrator aperture

(2)

Qr = Qs ·η0

(3)

Radiant solar energy falling on the receiver

Grash number based on length L

Useful energy collected

(13)

The amount of radiation from above the Earth on a simple surface is calculated as follows [32]:

Gon = Gsc [1 + 0.033 cos(360°n/365)]

(14)

where n refers to a specific day of the year and G is the solar constant, 1367 W/m2. The value of Gon on the horizontal plane is obtained by the following equation [32]:

H0 =

24 × 3600 × Gon πωs ⎛cos ϕ cos δ sin ωs + sin ϕ sin δ ⎞ π 180° ⎠ ⎝

(15)

δ = 23.45° sin(360° (284 + n)/365)

(16)

ωs = cos−1 ( −tan ϕ tan δ )

(17)

N=

(1)

η0 = λρταγ cos(θ) Optical efficiency

Grl = gβ (Tw − Ta

(10)

Qlr = Ac εeff σ (Tw4 − Ta4 ) Radiative heat loss through the receiver aperture

Solar dish collectors

) L3 / ν 2

(7)

The convective heat transfer coefficient

Qlc = hc Aw (Tw − Ta) Convective heat loss through the receiver aperture

specifications of the equipment in the IS. The highest power capacity is generated by ST100 turbine with 601 MW, and the lowest power is generated in the ST103 turbine with 107.7 MW.

Qs = Is Aa

(6)

2 ωs 15

(18)

N is equal to the monthly average amount of the maximum sunlight duration. KT has been calculated analogously to the presented procedure in the Ref. [32].

H = H0 KT ⇔ 1 ⩽ n ⩽ 365

(4)

(19)

The amount of total solar radiation on the horizontal surface can be 4

Sustainable Energy Technologies and Assessments 37 (2020) 100572

B. Ghorbani, et al.

Table 2 Specifications of temperature, pressure, and mass flow rate of streams in the IS. Stream

Temperature (°C)

Pressure (kPa)

Mass flow (kg/s)

Stream

Temperature (°C)

Pressure (kPa)

Mass flow (kg/s)

100 101 102 103 104 105 106 107 108 109 110 111 112 113 114 115 116 117 118 119 120 121 122 123 124 125 126 127 128 129 130 131 Oil1 Oil2

275.8 590.0 392.9 392.9 392.9 392.9 392.9 321.6 321.6 321.6 221.4 221.4 221.4 165.2 165.2 165.2 63.0 38.7 38.8 47.1 117.4 117.4 48.2 392.9 177.8 176.7 131.0 88.7 89.4 171.4 25.0 40.7 600.0 283.7

7204.9 7200.0 1704.7 1704.7 1704.7 1704.7 1704.7 926.9 926.9 926.9 344.7 344.7 344.7 183.3 183.3 183.3 183.3 6.9 386.1 386.1 183.3 344.7 344.7 1704.7 1704.7 926.9 926.9 344.7 7496.0 7349.0 101.3 101.3 200.0 180.0

1595.7 1595.7 1595.7 1403.0 192.6 1250.0 153.0 1250.0 1050.0 200.0 1050.0 1020.0 30.0 1020.0 1004.4 15.6 1004.4 1004.4 1004.4 1004.4 15.6 15.6 1020.0 345.6 345.6 545.6 545.6 1595.7 1595.7 1595.7 1542.9 1542.9 3602.5 3602.5

200 201 202 203 204 205 206 207 208 209 210 211 212 213 214 215 216 217 218 219 220 221 222 223 224 225 226 227 228 229 230 231 Oil3

122.0 82.2 62.9 56.3 68.0 62.9 62.9 62.9 68.0 68.0 63.4 56.3 64.5 64.5 64.5 64.5 60.5 56.3 61.0 61.0 61.0 61.0 56.3 61.0 61.0 61.3 60.9 52.1 25.0 56.3 56.3 56.3 283.7

80.0 29.1 26.1 29.9 25.9 26.1 26.1 80.0 25.9 25.9 22.9 26.1 22.1 22.1 22.1 22.1 19.1 22.7 18.7 18.7 18.7 18.7 97.3 18.7 18.7 19.1 18.7 15.7 101.3 97.3 97.3 97.3 250.0

1009.4 2883.9 2883.9 6171.6 6171.6 1009.4 1874.6 1009.4 2812.8 3358.8 2812.8 6171.6 6171.6 9530.4 2754.4 6776.0 2754.4 6171.6 6171.6 12947.6 2753.7 10193.9 6171.6 1874.6 879.1 7441.8 8320.9 8320.9 18514.8 18514.8 6171.6 6171.6 3602.5

throughout the year per hour in Bushehr.

obtained from the following Eq. [32]:

ω

Steam power plant

= 15 × ((h + 9.87 sin(2 × 360(n − 81)/364) − 7.53 × cos(360(n − 81)/364) − 1.5 sin(360° (n − 81)/364) − 4(120 − Llog ))/60 − 12)

The line 100 with temperature and pressure of 275.8 °C and 7205 kPa enters into the E100 heat exchanger (evaporator of the steam power plant) and exchange heat with the solar collector cycle. line 101 at 590 °C and 7200 kPa enters into the ST100 steam turbine and generate output power of 601 MW. Part of line 102 exited from ST100 is introduced into the ST101 steam turbine, and the rest is fed to the E101 heat exchanger to preheat the stream entered into the evaporator. The line 103 at 392.9 °C and 1705 kPa enters into the ST101 steam turbine generates 170.3 MW of power. The stream 107, exited from the ST101, is divided into two parts. About 84% of this stream enters into the ST102 steam turbine, and the rest is combined with the stream exited from the E101 heat exchanger and entered into the E102 heat exchanger. Stream 108 at 321.6 °C and 926.9 kPa is introduced into the ST102 steam turbine and produces power with the amount of 199.7 MW. Similarly, part of the streams exited from the steam turbine at 221.4 °C, and 3.447 kPa is fed into the ST103 steam turbine and produces 107.8 MW of power. About 98.47% of the output stream from the ST103 steam turbine is sent into the E104, and the rest is entered into the E109 for preheating. The stream of 114 which is at 165.2 °C and 183.3 kPa is delivered to the E104 and provides the required heat for the desalination system. The stream of 119 at 63 °C and 183.3 kPa enters into the E105 condenser so that it exchanges heat to the sea.

(20)

ω is defined as the hour angle. The transmitted solar radiation on the horizontal surface can be calculated as follows [32]

Id =

⎞ πHd ⎛ cos ω − cos ωs ⎜ ⎟ 24 ⎜ sin ωs − 2πωs cos ωs ⎟ 360° ⎝ ⎠

( )

(21)

Hd is defined as the daily solar radiation on the horizontal surface [32]:

0.99 KT ⩽ 0.17 ⎫ ⎧ ⎪ ⎪ 1.188 − 2.272KT + 9.473KT2− ⎪ 0.17 < KT < 0.75⎪ Hd = 21.865KT3 + 14.648KT4 ⎬ ⎨ H 0.75 < KT < 0.8 ⎪ − 0.54KT + 0.632 ⎪ ⎪ ⎪ 0.2 KT ⩾ 0.8 ⎭ ⎩

(22)

The heat supply structure of solar dish collector system is shown in red in Fig. 2. The Oil1 stream is containing BiPhenyl and diPH-Ether with a mole fraction of 24.62% and 75.38%; respectively. The stream is introduced at 600 °C and the input pressure of 200 kPa into the E100 heat exchanger, and with the temperature of 283.7 °C and the pressure of 180 kPa is exited. The solar collector system along with the auxiliary boiler transfer 3740 MW heat to the E100 heat exchanger (evaporator of power plant). Fig. 3 depicts the plot of solar radiation throughout the year per hour in Bushehr. Fig. 4 depicts the plot of ambient temperature changes

Multi-effect desalination system Multi-effect desalination (MED) systems take advantage of heat energy and are categorized in thermal processes. The system is considered as the first and foremost method of pure water production from 5

Sustainable Energy Technologies and Assessments 37 (2020) 100572

B. Ghorbani, et al.

Table 3 Specifications of the equipment in the IS. Pump

P100 P101 P102 P103 P104

Adiabatic Eff.

Power(kW)

ΔP (kPa)

P ratio (–)

0.8 0.8 0.8 0.8 0.8

477.5 87.84 14,897 410.9 3.366

379.2 53.92 7151 70.00 161.4

56.04 3.067 21.75 1.389 1.881

Adiabatic Eff.

Power (kW)

ΔP (kPa)

P ratio (–)

0.8 0.8 0.8 0.8

601,032 170,346 199,721 107,794

5495 777.8 582.2 161.4

0.2368 0.5437 0.3718 0.5317

Min. Approach (°C)

LMTD (°C)

Duty(kW)

Cold Pinch Temp. (°C)

7.9 6.370 10.31 58.62 1.114 13.74 6.613 3.456 3.531 4.62

12.90 38.21 17.68 77.04 13.61 17.69 9.958 15.09 13.89 12.71

3,740,740 856,388 585,797 36,153 2,571,772 105,451 7,136,069 6,877,502 6,753,641 2,523,998

275.7 171.4 171.4 38.77 62.88 25.00 56.26 64.51 60.96 56.25

Turbine

ST100 ST101 ST102 ST103 Heat Exchanger

E100 E101 E102 E103 E104 E105 E106 E107 E108 E109 Ejector Ejector

Suction Nozzle Size (mm)

Motive Nozzle Size (mm)

Discharge Nozzle Size (mm)

Pressure Drop (kPa)

Efficiency

200

250

300

50.92

0.98

Fig. 4. Ambient temperature changes throughout the year per hour in Bushehr. Fig. 3. Solar radiation throughout the year per hour in Bushehr.

223) is suctioned from the last effect, which causes the vacuum occurred in the system. The initial steam and the steam supplied by the ejector reach to the temperature of 82 °C and the input pressure of 29.1 kPa reaching the first stage by stream 201 (E106 heat exchanger). On the other hand, seawater (line 228), preheated by the condenser (E109), is fed as line 229 by dropping of pressure in the expansion valves into each stage. Injected streams by vapors entering the tubes are suddenly vaporized, and vapors in the tubes are also condensed. The steam from the first stage, after passing through the demister (D100 arrows), is led to the second stage (line 208). This steam with a lower temperature than the inlet temperature of the system (E107 heat exchanger) can evaporate the inlet water into the second stage (line 211),

seawater, operating under vacuum and condense seawater vapors, in which an ejector is used for creating of vacuum. Two streams are introduced to the system. One of which is the steam used by the system (line 201) and the other is the seawater (line 203). The steam used in the MED system is supplied by the waste heat recovery of the steam power plant in the E104 heat exchanger. In the MED system, the steam exited from the heat exchanger E104 (line 200) is sent into an ejector nozzle, which will cause a pressure drop due to the nozzle inside of the ejector. Since the central portion is connected to the final stage of the desalination system, due to the pressure drop, a steam amount (stream 6

Sustainable Energy Technologies and Assessments 37 (2020) 100572

B. Ghorbani, et al.

Table 5 Design specifications MED system. Design characteristics

Amount

Unit

The entrainment ratio of steam ejector Total brine Steam temperature last effect Gain output ratio (GOR) Relative saline water entering freshwater outlet Total received heat Total desalinated water Effect number Power consumption

2.601 10,194 60.96 2.885 2.225 2571 8321 3 87.84

kg.s−1/kg.s−1 kg/s °C kg.s−1/kg.s−1 kg.s−1/kg.s−1 MW kg/s – kW

Table 6 Design specifications for solar dish collector in the IS [6].

Fig. 5. net heat generation changes by solar collectors during a year.

Parameter

symbol

Value

Solar dish surface area

Aa

Un-shading factor Reflectivity from the surface of the solar dish The resulted transmittance-absorptance Receiver intercept factor Absorber characteristic length Geometric concentration ratio Thermal conductivity of the ambient air Cavity internal area of receiver

λ ρ τα γ L C K Aw φ1 εc

12.56m2 0.99 0.94 0.9 0.99 0.254 m 3000 0.025 W/m k

Cavity tilt angle Cavity surface emittance

Fig. 5 depicts the amount of power generated by solar collectors throughout the year. The IS requires a heat of 3740 MW, in which an auxiliary boiler is used to provide the required heat in addition to solar collectors. Fig. 6 depicts the heat generation variation by the auxiliary boiler in an IS for one year. Table 4 depicts the share of solar dish collectors for providing thermal energy of the IS is equal to 81.6%, and the efficiency of the steam generating power plant is equal to 28.84%, and total net heat efficiency is equal to 97.18%. Table 5 illustrates the design specifications of the MED system. The GOR value is the ratio of the mass flow rate of fresh water produced to the amount of steam entering the first water stage and is equal to 2.601. The three-stage desalination system can produce 8321 kg/s fresh water per 87.84 kW. Table 6 defines the design characteristics of solar collector collectors in the IS. Fig. 7 shows validation of different parts of the integrated structure relative to reference articles [27,33–36]. Energy balance equations for each equation are established with the help of the specific enthalpy [37,38]:

Fig. 6. heat generation changes by an auxiliary boiler in the IS during a year. Table 4 Design specifications for the entire developed IS. Parameters existing in the IS

Value

Production of thermal energy by solar dish collectors for a year Auxiliary amount of heat energy by urban gas for a year Share of solar dish collectors for providing required heat of

26,558 GWh 6205 GWh 81.06%

ISSF =

QUseful Q Axillary + QUseful

Heat stored in PCM for a year The number of solar dish collectors Net power generation of steam power plant for a year Power consumption of steam power plant for a year Power consumption of MED system for a year The rate of fresh water production Efficiency of steam power plant

ηSteam Power =

ηthermal =

13,279 GWh 720,000 9451 GWh 138.2 GWh 0.770 GWh 8320 kg/s 28.84%

Ẇ Turbine Q̇Evaporator

Net overall thermal efficiency

0.0645m2 π/2 0.92

∑ ṁ in hin − ∑ ṁ out hout − Ẇ 97.18%

in

̇ Ẇ Turbine + Wequal , inlet to Disalination − WPumps ̇ + Q̇Heater QSolar

+ Q̇ = 0

out

(23)

Apart from the loss of heat in heat exchanger, energy balance equations for each heat exchanger can be reported as follows [9]:

ṁ in, i (hin1, i − hin2, i ) = ṁ out , i (hout1, i − hout 2, i ) Tin1, i = Tout1, i + Δ Tin, HXi

and these are the important features of the MED system. Because at each stage, the pressure is reduced along with the temperature, it is possible to provide only the first stage steam in a MED system, and the vapor of the next steps will be provided according to the mechanism of the device. This process proceeds in the third step, and a portion of the last stage steam (line 224) along with the other fluids of each stage as the line 226 eventually enters into the condenser (E109). The nozzle suctions about 68.07% of the final vapor mass flow rate, and the inlet water condenses the remaining steam. In order to simulate the IS, the equations used in the reference [9] have been used. The schematic of MED system is shown in Fig. 2 in blue.

(24)

To write the equation of energy balance for pumps and turbines isentropic efficiencies is used, from that the Eqs. (25) and (26) are reported [39].

hout =

S hout − hin + hin ηs

S hout = (hout − hin ) ηs + hin

(25) (26)

Also, by writing the energy and mass balances in the mixture, the 7

Sustainable Energy Technologies and Assessments 37 (2020) 100572

B. Ghorbani, et al.

Fig. 7. Validation of different parts of the integrated structure relative to referenced articles [27,33–36]. Table 7 Design specifications for PCM system developed in Matlab. Inorganic substances with potential use as PCM (KCl/NaCl/MgCl2/ BaCl2)

Value

PCM solid density (kg/m3) PCM liquid density (kg/m3) TESpcm surface area relative to U (m2) Volume fraction of PCM in TESpcm TESpcm volume (m3) TESpcm loss coefficient (kW/m2K) PCM phase change enthalpy (kJ/kg) PCM melting temperature (˚C) PCM specific heat (kJ/kg.K) Initial temperature (˚C) Set-point (˚C)

2700 2642 2750 0.9000 6997 0.1600 560 485 1.038 608 400

following equations are reported [9]:

Fig. 8. Validation of temperature variations of the PCM system with the reported references [48–50]. 8

ṁ in,1 hin,1 + ṁ in,2 hin,2 = ṁ out hout

(27)

ṁ in,1 + ṁ in,2 = ṁ out

(28)

Sustainable Energy Technologies and Assessments 37 (2020) 100572

B. Ghorbani, et al.

dE (t ) E (t ) − E (t − Δt ) ̇ ≈ = ṁ l (t ). CHFT . (Tl (t ) − TTES (t − Δt )) − Qloss dt Δt (33)

dE (t ) E (t ) − E (t − Δt ) ≈ dt Δt ̇ = −ṁ u (t ). CHFT . (TTES (t − Δt ) − Tu (t )) − Qloss

(34)

The heat loss of the PCM tank to the environment is stated as follows:

̇ = U . A. (TTES (t − Δt ) − Tambient ) Qloss

(35)

It should be noted that, U, A, TTES and Tambiant are the total heat transfer coefficient, the heat transfer area, the temperature of the PCM tank, and the ambient temperature, respectively. Eqs. (36) and (37) show the phase of the material of interest for the phase change material, if E (t ) is less than EPCM,min the phase change material is the solid state and if the former greater than the later, the phase of the material is liquid.

Fig. 9. Changes in temperature and the amount of stored heat of PCM system with respect to time.

EPCM ,min = [(1 − ϕ). V . ρw . Cw. Tm] + [(ϕ. V ). ρPCM . CPCM . Tm]

(36)

EPCM ,max = EPCM ,min + [(ϕ. V ). ρPCM . hPCM ]

(37)

ϕ is volume coefficient ratio of the PCM, V(m ) is tank volume, ρw (kg/ m3) is water density, Cw)J/°C.kg) is water heat capacity, Tm(°C) is melting temperature of PCM, and ρPCM (kg/m3) is PCM density, CPCM (J/°C.kg) is PCM heat capacity, and hPCM (kJ/kg) is enthalpy of change phase. The amount of f coefficient that shows the state of PCM is calculated as follows: 3

if E (t ) < EPCM ,min ⎧0 ⎪ E (t ) − EPCM ,min if E f= E PCM ,min ⩽ E (t ) ⩽ EPCM ,max ⎨ PCM ,max − EPCM ,min ⎪1 if E (t ) > EPCM ,max ⎩

Figs. 9 and 10 show the changes in temperature and the amount of energy stored by the PCMs at different times. In this case, i.e. Fig. 9, the molten salt absorbs heat in storage state; as a result, the temperature rises from 400 to 608 °C, and the stored energy increases. Conversely, in the charging state depicted in Fig. 10, the outlet stream is returned and absorbed the thermal energy from PCM; therefore, its temperature is reduced.

Fig. 10. Changes in temperature and released heat rate of the PCM system with respect to time.

hout =

ṁ in,1 hin,1 + ṁ in,2 hin,2 ṁ in,1 + ṁ in,2

(29)

Exergy analysis

The Eqs. (30) and (31) by writing the conservation of mass and energy balance in the flash separator drum, the desired output can be extracted as follows [9]:

ṁ in hin = ṁ out ,1 hout ,1 + ṁ out ,2 hout ,2

(30)

ṁ in = ṁ out ,1 + +ṁ out ,2

(31)

Exergy is the energy which is obtainable to be used. The exergy is equal to zero when the system and surroundings reach equilibrium [41,42]. Exergy is presented by the following equation and divided into physical and chemical parts supposing that the potential, kinetic, and the other forms of energy are unchanged or insignificant [43,44] :

e = e ph + e ch

According to the first law of thermodynamics, the process of throating is enthalpy constant. Therefore:

hin = hout

(38)

(39)

Physical exergy is obtained by the following equation [45,46]:

e ph = (h − h°) − T° (s − s°)

(32)

(40)

where h° is enthalpy and S° is entropy in the standard state. Chemical exergy rate of the mixture is obtained by [47]:

e ch =

Modeling of phase change materials system

∑ xi ei0 + RT0 ∑ xi lnxi γi

(41)

In Eq. (35), γi stands for the component activity factor. It is also [46] possible to calculate the chemical exergy by Eq. (36).

This paper uses phase change materials to store thermal energy during the day, and release the stored heat during the night on June 20. Fig. 8 shows the changes in temperature and the amount of energy stored by the PCMs of the reference articles and the code developed in this paper at different times. Table 7 shows the physical properties of the PCM design [40]. In order to simulate phase change materials, energy equations are used when the system is charging and discharging [29]:

e ch =

∑ xi ei0 + G − ∑ xi Gi

(42)

Table 8 depicts the different exergy values of streams in the IS. Table 9 displays the fuel, product and the exergy destruction in each equipment of the IS. Table 9 depicts that the E100 is responsible for the highest rate of exergy destruction with 179108.1 kW and the E105 has 9

Sustainable Energy Technologies and Assessments 37 (2020) 100572

B. Ghorbani, et al.

Table 8 Physical, chemical, and total exergy of all streams in the IS. Stream

Rate of Physical Exergy (kW)

Rate of Chemical Exergy (kW)

Rate of Total Exergy (kW)

Stream

Rate of Physical Exergy (kW)

Rate of Chemical Exergy (kW)

Rate of Total Exergy (kW)

100 101 102 103 104 105 106 107 108 109 110 111 112 113 114 115 116 117 118 119 120 121 122 123 124 125 126 127 128 129 130 131 Oil1 Oil2

550144.4 2430360.5 1759739.6 1547278.3 212461.3 1378544.5 168733.8 1186549.0 996701.2 189847.8 766122.9 744233.7 21889.2 617820.7 608390.4 9430.2 9789.8 1219.5 1673.3 3723.0 812.6 815.8 4071.3 381195.1 46324.7 230678.4 37216.9 41731.8 55964.7 207706.3 0.0 2672.6 2608729.3 549405.1

276350.0 276350.0 276350.0 242985.0 33365.0 216487.0 26498.0 216487.0 181849.1 34637.9 181849.1 176653.4 5195.7 176653.4 173957.0 2696.4 173957.0 173957.0 173957.0 173957.0 2696.4 2696.4 176653.4 59863.0 59863.0 94500.9 94500.9 276350.0 276350.0 276350.0 5496643.5 5496643.5 105588.6 105588.6

826494.4 2706710.4 2036089.6 1790263.3 245826.3 1595031.5 195231.9 1403036.0 1178550.3 224485.8 947972.0 920887.0 27084.9 794474.1 782347.4 12126.6 183746.8 175176.5 175630.3 177680.0 3509.0 3512.2 180724.7 441058.1 106187.7 325179.3 131717.8 318081.8 332314.6 484056.3 5496643.5 5499316.1 2714317.9 654993.7

200 201 202 203 204 205 206 207 208 209 210 211 212 213 214 215 216 217 218 219 220 221 222 223 224 225 226 227 228 229 230 231 Oil3

495352.3 971968.4 28621.6 40724.2 935245.2 10017.6 18604.0 10085.9 892818.7 39964.5 28724.5 40698.9 843412.8 882975.0 812167.1 68549.8 24109.1 40676.4 767201.4 834969.2 746950.1 85872.6 41173.2 508484.4 238465.7 71296.9 309714.4 42685.3 0.0 123519.7 41173.2 41,173 549758.1

3797079.3 10848798.0 10848798.0 22457208.7 22457208.7 3797079.3 7051718.7 3797079.3 10581097.2 11878573.6 10581097.2 22457208.7 22457208.7 34335949.1 10361493.9 23976714.8 10361493.9 22457276.1 22457276.1 46434267.0 10358787.8 36077628.7 22457208.7 7051718.7 3307069.1 27994309.8 31301378.9 31301378.9 67371693.6 67371693.6 22457208.7 22,457,276 105588.6

4292431.6 11820766.4 10877419.6 22497933.0 23392454.0 3807096.9 7070322.8 3807165.2 11473915.9 11918538.1 10609821.7 22497907.6 23300621.5 35218924.1 11173661.0 24045264.7 10385603.0 22497952.5 23224477.5 47269236.1 11105737.9 36163501.4 22498381.9 7560203.1 3545534.8 28065606.7 31611093.3 31344064.2 67371693.6 67495213.3 22498381.9 22,498,449 655346.6

Table 9 Fuel, product and destroyed exergy of equipment in the IS. Equipment

EḞ (kW )

EṖ (kW )

EḊ (kW )

Equipment

EḞ (kW )

EṖ (kW )

EḊ (kW )

E100 E101 E102 E103 E104 E105 E106 E107 E108 E109 Collectors ST100 ST101 ST102

3540812.3 932682.0 657494.0 187756.9 4589512.6 5680390.3 34318699.4 33971823.5 33671613.4 98982786.9 3299369.2 2706710.4 1595031.5 1178550.3

3361704.1 925114.4 615774.1 181189.0 4476178.4 5674492.6 34269873.6 33910443.2 33610080.5 98839277.6 2714317.9 2637122.0 1573382.8 1147693.6

179108.1 7567.7 41719.9 6568.0 113334.2 5897.7 48825.8 61380.3 61533.0 143509.4 585051.4 69588.5 21648.6 30856.6

ST103 P100 P101 P102 P103 P104 D100 D101 D102 V100 V101 V102 Ejector

920887.0 175654.1 3807184.7 347212.4 655404.7 3512.3 23392454.1 35218926.1 47269239.6 22498381.9 22498381.9 22498449.4 11852634.7

902268.4 175176.5 3807165.2 318081.8 655346.6 3512.2 23392454.0 35218925.7 47269239.3 22497933.0 22497907.6 22497952.5 11820766.4

18618.7 23.8 19.5 665.0 58.0 0.1210 0.1234 0.4231 0.3333 449.0 474.3 497.0 31868.3

highest exergy efficiency belongs to ST100 turbine with 89.62%, and the lowest exergy efficiency belongs to ST103 with 85.27% among all steam turbines. The highest exergy efficiency belongs to V101 with 84.32%, and the lowest exergy efficiency belongs to V102 with 45.31% among all expansion valves. The total exergy efficiency of the entire system is equal to 52.23%.

the least exergy destruction with 5897.7 kW among all heat exchangers. Among steam turbines, the ST100 turbine has the highest rate of exergy destruction with 69588.5 kW, and turbine ST103 has the least exergy destruction rate with 18618.7 kW. Fig. 11 depicts that the highest amount of exergy destruction in equipment belongs to heat exchangers, solar collectors, and steam turbines. Additionally, the share of the exergy destruction of the heat exchangers has also been shown in this figure. Table 10 depicts the exergy efficiency of the equipment in the IS. This table depicts that in the IS, the heat exchangers have the highest exergy efficiency among equipment, and the exergy efficiency of the expansion valve among the equipment is the lowest. The highest exergy efficiency belongs to the E107 with 99.32% and the lowest exergy efficiency belongs to E102 with 66.98%, among all heat exchangers. The

Sensitivity analysis Fig. 12 depicts the changes in the irreversibility and exergy efficiency of the IS during different hours of the year. Fig. 12 depicts that the rate of exergy destruction in the IS in the hot days of the year decreases with ambient temperature, and the exergy efficiency of the IS increases with temperature. These variations can be referred to the 10

Sustainable Energy Technologies and Assessments 37 (2020) 100572

B. Ghorbani, et al.

Fig. 12. Irreversibility changes and exergy efficiency of the IS during different hours of the year.

Fig. 14 depicts the amount of total exergy efficiency and the net power output variations concerning the surging in the number of solar dish collectors. With the increase in the number of collectors, the rate of heat transferred with the IS is increased, and thus the net production capacity of the IS and the amount of fresh water produced are also increased. On the other hand, according to the exergy equation of solar collectors presented in Table 4, the total exergy efficiency of the system reduces, as the rate of increasing in exergy is higher than the power generation and freshwater production. Fig. 15 depicts variations of net thermal efficiency and pure water production versus surging in the number of solar dish collectors in the IS. Due to the increase in the heat transferred into the IS, the production capacity and the equivalent heat which is transferred to the desalination system increase, thus the total net thermal efficiency is also increased. Fig. 16 shows variations of inlet energy to the steam cycle evaporator with respect to the number of solar dish collectors on June 20.

Fig. 11. The share of the exergy destruction of each equipment in the IS.

inputs exergy equation of collectors according to table 4. Fig. 13 also depicts the number of irreversibility changes and exergy efficiency of solar collectors. Table 10 Exergy efficiency of equipment in an IS. Components and exergy efficiency expression

Component identifier

Exergy efficiency (%)

Component identifier

Exergy efficiency (%)

Heat exchanger [51,52]

E100 E101 E102 E103 E104 ST100 ST101

95.21 99.12 66.98 81.83 95.59 89.62 88.72

E105 E106 E107 E108 E109 ST102 ST103

94.41 99.32 99.11 99.09 94.31 86.62 85.27

P100 P101 P102 V100 V101

95.02 77.81 95.54 56.73 84.32

P103 P104

85.88 95.96

V102

45.31

m

n

ηex

⎧ ∑1 (ṁ Δe) ⎫ ⎧ ∑1 (ṁ Δe) ⎫ ⎤ =1−⎡ ⎢ ⎨ ∑1n (ṁ Δh) ⎬ − ⎨ ∑1m (ṁ Δh) ⎬ ⎥ ⎭h ⎩ ⎭c ⎦ ⎣⎩

Turbine [51]

ηex =

W ∑ (ṁ . e )i − ∑ (ṁ . e )o

Pumps [53]

ηex =

∑ (ṁ . e )i − ∑ (ṁ . e )o W

Expansion valves

e ΔT

T0

=∫

ηex =

T − T0 dh , T

e Ph

=

e ΔT

+

e Δp

T eoΔT − eiΔT Δp Δp ei − eo

Ejector

ηex =

Ejector

99.73

Collectors

82.27

ηTotal

52.23

∑ (ṁ . e )o ∑ (ṁ . e )i

Collectors [14,54,55] 4T Exṡ = ⎡1 − a (1 − 0.28 ln f ) ⎤ Qṡ 3 Ts ⎦ ⎣ Eẋs is input solar exergy

ηex =

∑ (ṁ . e )o ∑ (ṁ . e )i

Cycle

ηex = 1 −

Totalirreversibilityincycle Totalconsumedpowerincycle

11

Sustainable Energy Technologies and Assessments 37 (2020) 100572

B. Ghorbani, et al.

Fig. 13. Irreversibility changes and exergy efficiency of collectors during different hours of the year.

Fig. 16. Variations of inlet energy to the steam cycle evaporator with respect to the number of solar dish collectors on June 20.

collectors and auxiliary boilers have been used to provide the required heat for the steam power plant. The PCM storage is employed during the night and in the absence of solar thermal sources. The IS has the capability of producing 1064 MW net power and 8321 kg/s of fresh water. Two indicators of lost work and exergy efficiency of equipment should be investigated in order to better compare the performance of different equipment of each process. By comparing the lost work and the efficiency of the various equipment of a process, it is possible to identify the points of the process in which energy is not effectively used and wasted, as it is the purpose of the exergy analysis. The heat exchangers have the highest amount with the exergy destruction of 46.83%. The highest rate of exergy destruction among the heat exchangers occurs in the E100. The heat exchanger has the highest rate of exergy destruction due to the difference between the cold and hot streams in the composite curve (temperature-enthalpy). Heat exchangers have higher exergy efficiency compared to the other equipment, while they have a high degree of irreversibility. The irreversibility of equipment such as expansion valves can be very low, yet they have low efficiency. This shows that the performance of the equipment should be analyzed simultaneously regarding irreversibility and exergy efficiency. Moreover, the production capacity of turbines is become higher the by dropping the exergy destruction of turbines; therefore, the exergy destruction rate in turbines should be minimized. The turbine shares of exergy destruction in the IS compared to other equipment is 9.84%. About the above items, the design of the equipment is carried out appropriately in IS. The IS sensitivity analysis depicts that with 88.89% surging in the number of solar collectors, the net production capacity of the IS in increased by 90.19%, the total system exergy efficiency is decreased by 33.76%, the production of fresh water is increased by 91.46%, and the total thermal efficiency of the IS is increased by 14.94%.

Fig. 14. Variations of exergy efficiency and net power generation versus surging in the number of solar dish collectors.

Fig. 15. Variations of net thermal efficiency and pure water production versus surging in the number of solar dish collectors.

Declaration of Competing Interest The authors declare that they have no known competing financial interests or personal relationships that could have appeared to influence the work reported in this paper.

The highest amount of inlet energy which is about 3700 MW is obtained with 720,000 collectors at 12 am.

References

Conclusion

[1] Maleki A, Askarzadeh A. Optimal sizing of a PV/wind/diesel system with battery storage for electrification to an off-grid remote region: A case study of Rafsanjan, Iran. Sustainable Energy Technologies and Assessments 2014;7:147–53. [2] Razmjoo A, Davarpanah A. Developing various hybrid energy systems for residential application as an appropriate and reliable way to achieve Energy sustainability. Energy Sources Part A 2019;41(10):1180–93. [3] Bakhtiar A, Aslani A, Hosseini SM. Challenges of Diffusion and Commercialization

One of the most important goals in the integration of the thermal power plants and desalination system is to increase the energy efficiency of the power plant in addition to fresh water production. In this paper, the waste energy of a steam power plant is employed for the production of fresh water in a three-effect desalination system. Solar 12

Sustainable Energy Technologies and Assessments 37 (2020) 100572

B. Ghorbani, et al.

[30] Pavlovic S, et al. Comparative study of spiral and conical cavity receivers for a solar dish collector. Energy Convers Manage 2018;178:111–22. [31] Ashouri M, et al. Thermodynamic and economic evaluation of a small-scale organic Rankine cycle integrated with a concentrating solar collector. International Journal of Low-Carbon Technologies 2015;12(1):54–65. [32] Mehdi Mehrpooya BG, Sina Hossieni Seyed. Thermodynamic and economic evaluation of a novel concentrated solar power system integrated with absorption refrigeration and desalination cycles. Energy Convers Manage 2018;1(12). [33] Moradi M, Mehrpooya M. Optimal design and economic analysis of a hybrid solid oxide fuel cell and parabolic solar dish collector, combined cooling, heating and power (CCHP) system used for a large commercial tower. Energy 2017;130:530–43. [34] Sabziparvar AA. A simple formula for estimating global solar radiation in central arid deserts of Iran. Renewable Energy 2008;33(5):1002–10. [35] Wu S-Y, et al. A parabolic dish/AMTEC solar thermal power system and its performance evaluation. Appl Energy 2010;87(2):452–62. [36] Wang Y, Lior N. Performance analysis of combined humidified gas turbine power generation and multi-effect thermal vapor compression desalination systems—Part 1: The desalination unit and its combination with a steam-injected gas turbine power system. Desalination 2006;196(1–3):84–104. [37] Lotfi B, et al. 3D numerical investigation of flow and heat transfer characteristics in smooth wavy fin-and-elliptical tube heat exchangers using new type vortex generators. Energy 2014;73:233–57. [38] Noroozian A, et al. Energy, exergy and economic analyses of a novel system to recover waste heat and water in steam power plants. Energy Convers Manage 2017;144:351–60. [39] Amidpour M, et al. Sensitivity analysis, economic optimization, and configuration design of mixed refrigerant cycles by NLP techniques. J Nat Gas Sci Eng 2015;24:144–55. [40] Cárdenas B, León N. High temperature latent heat thermal energy storage: Phase change materials, design considerations and performance enhancement techniques. Renew Sustain Energy Rev 2013;27:724–37. [41] Aghniaey S, Mahmoudi SMS. Exergy analysis of a novel absorption refrigeration cycle with expander and compressor. Indian Journal of Scientific Research 2014;1:815–22. [42] Ghorbani B, et al. Exergoeconomic analysis and multi-objective Pareto optimization of the C3MR liquefaction process. Sustainable Energy Technol Assess 2016;17:56–67. [43] Ehyaei M, Rosen MA. Optimization of a triple cycle based on a solid oxide fuel cell and gas and steam cycles with a multiobjective genetic algorithm and energy, exergy and economic analyses. Energy Convers Manage 2019;180:689–708. [44] Ghorbani B, et al. Simulation and optimization of refrigeration cycle in NGL recovery plants with exergy-pinch analysis. J Nat Gas Sci Eng 2012;7:35–43. [45] Mirzaei M, et al. Energy, exergy and economics analysis of an ORC working with several fluids and utilizes smelting furnace gases as heat source. Thermal Science and Engineering Progress 2018;5:230–7. [46] Ghorbani B, et al. Applying an integrated trigeneration incorporating hybrid energy systems for natural gas liquefaction. Energy 2018;149:848–64. [47] Mehrpooya M, Ghorbani B, Hosseini SS. Thermodynamic and economic evaluation of a novel concentrated solar power system integrated with absorption refrigeration and desalination cycles. Energy Convers Manage 2018;175:337–56. [48] Dadollahi M, Mehrpooya M. Modeling and investigation of high temperature phase change materials (PCM) in different storage tank configurations. J Cleaner Prod 2017;161:831–9. [49] Tay N, et al. Investigation of the effect of dynamic melting in a tube-in-tank PCM system using a CFD model. Appl Energy 2015;137:738–47. [50] Mehrpooya M, Ghorbani B, Sadeghzadeh M. Hybrid solar parabolic dish power plant and high-temperature phase change material energy storage system. Int J Energy Res 2019;43(10):5405–20. [51] Ghorbani B, et al. Cascade refrigeration systems in integrated cryogenic natural gas process (natural gas liquids (NGL), liquefied natural gas (LNG) and nitrogen rejection unit (NRU)). Energy 2016;115, Part 1:88–106. [52] Ghorbani B, Hamedi M-H, Amidpour M. Development and optimization of an integrated process configuration for natural gas liquefaction (LNG) and natural gas liquids (NGL) recovery with a nitrogen rejection unit (NRU). J Nat Gas Sci Eng 2016;34:590–603. [53] Mohammadi A, et al. Exergy analysis of a Combined Cooling, Heating and Power system integrated with wind turbine and compressed air energy storage system. Energy Convers Manage 2017;131:69–78. [54] Naseri A, et al. Exergy analysis of a hydrogen and water production process by a solar-driven transcritical CO2 power cycle with Stirling engine. J Cleaner Prod 2017;158:165–81. [55] Naseri A, Bidi M, Ahmadi MH. Thermodynamic and exergy analysis of a hydrogen and permeate water production process by a solar-driven transcritical CO2 power cycle with liquefied natural gas heat sink. Renewable Energy 2017;113:1215–28.

of Bioenergy in Developing Countries. Renewable Energy 2019. [4] Lior N. Advances in water desalination Vol. 1. John Wiley & Sons; 2012. [5] Khawaji AD, Kutubkhanah IK, Wie J-M. Advances in seawater desalination technologies. Desalination 2008;221(1–3):47–69. [6] Leiva-Illanes R, et al. Exergy cost assessment of solar trigeneration plant based on a concentrated solar power plant as the prime mover. AIP Conf Proc 2019;2126(1):230001. [7] Shadmehri M, et al. Numerical simulation of a concentrating photovoltaic-thermal solar system combined with thermoelectric modules by coupling Finite Volume and Monte Carlo Ray-Tracing methods. Energy Convers Manage 2018;172:343–56. [8] Ariyanfar L, Yari M, Abdi Aghdam E, Energy. exergy, economic, environmental (4E) analyses of a solar organic Rankine cycle to produce combined heat and power. Modares. Mechanical Engineering 2016;16(10):229–40. [9] Mehrpooya M, Ghorbani B, Mousavi SA. Integrated power generation cycle (Kalina cycle) with auxiliary heater and PCM energy storage. Energy Convers Manage 2018;177:453–67. [10] Shakib SE, Amidpour M, Aghanajafi C. Simulation and optimization of multi effect desalination coupled to a gas turbine plant with HRSG consideration. Desalination 2012;285:366–76. [11] Hosseini SR, Amidpour M, Shakib SE. Cost optimization of a combined power and water desalination plant with exergetic, environment and reliability consideration. Desalination 2012;285:123–30. [12] Ashouri M, et al. Techno-economic assessment of a Kalina cycle driven by a parabolic Trough solar collector. Energy Convers Manage 2015;105:1328–39. [13] Amelio M, et al. An evaluation of the performance of an integrated solar combined cycle plant provided with air-linear parabolic collectors. Energy 2014;69:742–8. [14] Ahmadi G, Toghraie D, Akbari OA. Solar parallel feed water heating repowering of a steam power plant: a case study in Iran. Renew Sustain Energy Rev 2017;77:474–85. [15] Maleki A, Pourfayaz F, Ahmadi MH. Design of a cost-effective wind/photovoltaic/ hydrogen energy system for supplying a desalination unit by a heuristic approach. Sol Energy 2016;139:666–75. [16] Mohammadi A, et al. Thermoeconomic analysis and multiobjective optimization of a combined gas turbine, steam, and organic Rankine cycle. Energy Sci Eng 2018;6(5):506–22. [17] Ahmadi MH, et al. Designing a powered combined Otto and Stirling cycle power plant through multi-objective optimization approach. Renew Sustain Energy Rev 2016;62:585–95. [18] Jokar MA, et al. Thermodynamic evaluation and multi-objective optimization of molten carbonate fuel cell-supercritical CO2 Brayton cycle hybrid system. Energy Convers Manage 2017;153:538–56. [19] Javadi Z, Miansari M, Ghorbani B. Retrofit of steam power plant by using solar dish collectors and multi-effect desalination cycle (exergy and economic analysis). Modares Mechanical Engineering 2019;19(12). [20] Piadehrouhi F, et al. Development of a new integrated structure for simultaneous generation of power and liquid carbon dioxide using solar dish collectors. Energy 2019;179:938–59. [21] Manesh MK, Amidpour M. Multi-objective thermoeconomic optimization of coupling MSF desalination with PWR nuclear power plant through evolutionary algorithms. Desalination 2009;249(3):1332–44. [22] Peng S, et al. Exergy evaluation of a typical 330 MW solar-hybrid coal-fired power plant in China. Energy Convers Manage 2014;85:848–55. [23] Blumberg T, et al. Comparative exergoeconomic evaluation of the latest generation of combined-cycle power plants. Energy Convers Manage 2017;153:616–26. [24] Akbari M, et al. Energy and exergy analyses of a new combined cycle for producing electricity and desalinated water using geothermal energy. Sustainability 2014;6(4):1796–820. [25] Ansari K, Sayyaadi H, Amidpour M. Thermoeconomic optimization of a hybrid pressurized water reactor (PWR) power plant coupled to a multi effect distillation desalination system with thermo-vapor compressor (MED-TVC). Energy 2010;35(5):1981–96. [26] Meratizaman M, et al. Scenario analysis of gasification process application in electrical energy-freshwater generation from heavy fuel oil, thermodynamic, economic and environmental assessment. Int J Hydrogen Energy 2015;40(6):2578–600. [27] Reyhani HA, et al. Thermodynamic and economic optimization of SOFC-GT and its cogeneration opportunities using generated syngas from heavy fuel oil gasification. Energy 2016;107:141–64. [28] Mehrpooya M, Ghorbani B, Sadeghzadeh M. Hybrid solar parabolic dish power plant and high-temperature phase change material energy storage system. Int J Energy Res 2019. [29] Ghorbani B, Mehrpooya M, Sharifzadeh MMM. Introducing a hybrid photovoltaicthermal collector, ejector refrigeration cycle and phase change material storage energy system (Energy, exergy and economic analysis). Int J Refrig 2019;103:61–76.

13