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## Exergetic, Exergoeconomic and Exergoenvironmental Multi-Objective Genetic Algorithm Optimization of Qeshm Power and Water Cogeneration Plant | |||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||

Gas Processing | |||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||

مقاله 1، دوره 7، شماره 2، زمستان 2019، صفحه 1-28
اصل مقاله (1.56 MB)
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شناسه دیجیتال (DOI): 10.22108/gpj.2019.119381.1066 | |||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||

نویسندگان | |||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||

Hossein Vazini Modabber؛ Mohammad Hassan Khoshgoftar Manesh ^{}
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^{}1 Division of Thermal Science & Energy Systems, Department of Mechanical Engineering, Faculty of Technology & Engineering, University of Qom, Qom, Iran 2 Center of Environmental Research, University of Qom, Qom, Iran | |||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||

چکیده | |||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||

In this study, optimization of Qeshm power and water desalting cogeneration plant has been investigated. The objective functions are related to maximizing exergetic efficiency and minimization of exergoeconomic and exergoenvironmental parameters. Also, the integration of RO desalination with the existing plant has been evaluated based on these analyses. This plant includes two MAPNA 25 MW gas turbines, two heat recovery steam generators, and two MEDTVC desalination units. Thermodynamic modeling and simulation of the plant have been performed in MATLAB software. The thermodynamic simulation verified by Thermoflex software and plant data with high accuracy. Also, the computer code has been developed to perform exergetic, exergoeconomic and exergoenvironmental analysis. Multi-Objective Genetic Algorithm (MOGA) has been applied to find optimum objective functions and decision variables based on exergetic, exergoeconomic and exergoenvironmental parameters. Results show that in the optimum plant overall exergetic efficiency of the plant has been increased by 27.78%, and total exergetic cost and total exergoenvironmental impacts have been decreased by 0.93% and by 0.89%. | |||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||

کلیدواژهها | |||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||

Cogeneration؛ MEDTVC Desalination؛ RO Desalination؛ Exergy Analysis؛ Exergoeconomic Analysis؛ Exergoenvironmental Analysis | |||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||

اصل مقاله | |||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||

**Introduction**
Freshwater means water that contains less than 1000 milligrams of salinity per liter of water [1]. However, most of the water present on the surface of the earth has a salinity of up to 10,000 ppm, and the free water is usually salinity in the range of 35,000 ppm to 45,000 ppm in the form of salts dissolved in water [2]. Our country is no exception. On the other hand, the shortage of Freshwater resources in Iran and, on the other hand, access to saltwater resources of the Persian Gulf in the south, and the Caspian Sea in the north, necessitate the need for Freshwater supply from these resources for industrial, and domestic uses.The issue of Desalination has attracted attention in most countries of the world in recent years. Today, over 15,000 units of desalinating water units are operating around the world. The Middle East accounts for roughly 50% of the world's total freshwater production. Saudi Arabia, with about 26% of world freshwater production capacity, is the largest producer in the industry, and the United States with 17% is in the next category. In Saudi Arabia, thermal water desalination is most used[1]. The process of separating salt from saline water, like any other process, requires energy, and the amount of this energy is different for different methods of desalination. In a particular process, the amount of energy per unit volume of Freshwater produced depends on the chemical composition and degree of impurities of saline water and its thermodynamic characteristics[3]. Lack of energy and high and continuous costs of energy supply increased energy consumption, environmental pollution due to the consumption of fossil fuels and the deterioration of fossil fuels has led to issues of energy recovery in industrial and process units in recent years[4-8].There is some investigation related to energy reduction in the process industries in Iran by exergy analysis. The identification of the sources of energy losses by the exergy method for the Marun Mega-Olefin petrochemical complex has been done by Paashang et al [9]. Ghorbani et al investigated an integrated nitrogen rejection unit with LNG and NGL co-production processes based on the MFC and refrigeration systems through exergoeconomic analysis [10]. Ghazizadeh et al studied C3MR, MFC and DMR refrigeration cycles in an integrated cryogenic process with advanced exergoeconomic analysis [11]. An advanced exergetic analysis of the integrated separation process with considering optimization refrigeration system has been investigated by Hamedi et al [12].Sheikhi et al applied pinch and exergy analysis for optimization of the refrigeration cycle in the petrochemical complex [13]. Optimization of an integrated process conﬁguration for IGCC with a Fischer-Tropsch has been evaluated with coal and biomass fuels by Shariati Niassar[14]. In the other research, Hadadi et al performed and evaluated optimization of water and wastewater network related to a gas refinery with considering pressure drop and pumping cost using conceptual, mathematical and evolutionary methods[15]. Exergoeconomic and environmental optimization of a 160 MW combined cycle power plant through MOEA has been done by KhoshgoftarManesh and Babaelahi[16]. Over the years, extensive research has been done on power generation systems anddesalination systems. Tadros assessed the combination of a multi-stage flash (MSF) desalination unit with a variety of steam turbines, as well as a gas turbine, and boiler, in 1979, due to the extensive use of multi-effectdesalination. In the study, the economics of these systems, and thermodynamic characteristics were studied and optimization studies were carried out. The results have shown that a single unit of MSF can produce up to 1400 m In 2014, Alzahrani et al. has been investigated a gas turbine cycle integrated with MEDTVC desalination and RO units. An energy recovery device related the thermal desalination unit to the gas turbine cycle. An exergy analysis has been performed to show the destruction of each component. Effect No.4 of the MED thermal desalination unit has 45% of the total exergy destruction [28]. In 2015, Eshoul et al. has considered a combined cycle power plant standalone and integrated with a MEDTVC desalination unit. They performed thermodynamic and exergy analyses on the case study. Also, the amount of the environmental impact as carbon dioxide has been obtained and the results show that the emission rises by increasing the ambient air temperature. Every 10°C increase in the ambient air temperature rises the plant efficiency by about 0.42% and decreases the output power about 5.3%[29]. In 2018, Eshoul et al. has considered a MEDTVC desalination unit lonely and done energetic, exergetic, and economic analysis on it. The results show that thermocompressor is the main source of the exergy destruction in this system. By using a preheater in this system, the cost of the desalinated water has been decreased [30]. In four papers, Kamali et al. [31-34] developed and then optimized a model for thermodynamic simulation of a multi-stage desalination. The developed model is then compared and validated with the experimental data of one of the Kish Island desalination currently in operation. The developed model is based on the basics of the design of the cell shell transducers, although there is no discussion of the economic aspects of the system under study in their research. Also, the impact of the required vapor suction site from the country on the optimal desalination performance is evaluated. Several researchers have also focused more on MED, MSF, and RO desalination systems, as well as the combined use of these desalination. Muginstein et al. [35] are evaluated the performance of two reverse osmosis desalination and multi-stage desalination steam desalination both desalination was connected to a combined cycle power plant. Darwish et al. [36] Given the shortage of freshwater in Kuwait, they suggested the use of gas turbines to produce freshwater, all of the researchers' multi-stage desalination plants were of a multi-stage type with a sudden pressure drop to the turbine. In this paper, the researchers investigated many combinations between thermal desalination and reverse osmosis with thermal power plants. Most of this paper focuses on general engineering calculations and does not include process modeling and simulation.Messineo et al. [37] also conducted a study similar to the work of Cardona et al. [38] except that there was no thermal coupling between multistage distillate desalination, reverse osmosis desalination, and only freshwater of these two freshwaters mix to get the desired quality of acid.Rensonnet et al. [39] also studied the various configurations of the combination of multistage distillation desalination and reverse osmosis desalination and thermoeconomic power plants. Mokhtari et al evaluated (GT + MED + RO) hybrid system for desalination in the Persian Gulf. Promotion in performance of a GT + MED + RO to achieve more water production capacity Talebbeydokhti etal performed evaluation and optimization low-temperature MED system powered by CSP. The selection of integrated LT-MED with CSP-DEC is investigated [40]. Dynamic simulation of MED-TVC desalination integrated with nuclear reactor with high modeling accuracy has been performed by Dong et al. A lumped-parameter for nuclear desalination plant has been considered [41]. Performance evaluation of an auto-tuning area ratio ejector for the MED-TVC desalination process has been proposed by Gu et al [42]. Evaluation of varying motive steam to performance are considered. Elsayed et al investigated a transient simulation of MED desalination with different feed configurations[43]. Backward feed, forward feed, parallel feed and parallel/crossfeed are considered. MED-TVC with parallel/crossfeed has the best response. The integration of MED with the solar Rankin cycle powered by the linear fresnel solar field has been proposed by Askari and Ameri. In this regard, fuel consumption is reduced significantly by using the solar energy[44]. Dynamic modeling of a MED-TVC plant has been proposed by Guimard et al [45]. A dynamic model based on mathematical equations has been implemented. Also, transient operations related to disturbances are considered. Based on the brine levels in the effects Strategies for process control under modification of regimes have been developed. Shayesteh et al investigated to find 4E optimum the ORC-RO system parameters for Water–Energy-Environment nexus. In this regard, the environmental impacts index has been defined for the RO system [46].Palenzuela et al evaluated based on Techno-Economic analysis between CSP+MED and CSP+RO in MENA Region[47]. As mentioned before, there is no study about simultaneous exergetic, exergeoconomic and exergoenvironmentthree-objectives optimization for power and desalination plants. In this study, the Qeshm cogeneration plant with the gas turbine, HRSG and MEDTVC has been selected as a real case study to find optimum conditions based on Multi-Objective Genetic Algorithm (MOGA). In this regard, exergetic, exergoeconomic and exergoenvironmental optimization of Qeshm power and desalting plant have been investigated
**Case study**
The Qeshmpower/water cogeneration plant includes two MAPNA 25 MW gasturbines, two Heat Recovery Steam Generators (HRSG) and two MED-TVC desalination units. The technical characteristics of the Qeshm power/water cogeneration plant is indicated in table 1. As shown in Figure 1, the integrated RO with existing MED-TVC plant are investigated.
**Methodology**
Thermodynamics means studying energy, turning energy into different modes, and the ability to work energy. At first, three thermodynamic laws were drafted, but according to the fourth law, the so-called zeroth law was called, because the law had one, two, three, and it was not a fundamental principle. Many power plants and heat engines generate useful work by converting energy. In all of them, energy translates into a mechanical component and leads to the production of work. This energy conversion is based on the first law of thermodynamics. Mass and energy balances for each component are given as equation (1) & (2)[48, 49]:
The base thermodynamic equations of each component are expressed in Table 2, 3, 4, and5 respectively as follow. The number of water desalination unit equations that must be solved simultaneously is relatively high because all of these equations must be solved in the number n of the simultaneous operation that increases the number of involved equations. On the other hand, the user in the analysis input, which makes the coding more complex, and requires more flexibility, can change the number of effects. Therefore, to provide this flexibility, MED coding modeling is used in the EES software environment. Nevertheless, the rest is coding in the MATLAB software environment. This decision is causing a disruption in the simultaneous implementation of the code developed in both software, which is not desirable; because we intend to analyze all parts of the system simultaneously with the implementation of the model, and the results of one section, on effect other sectors. To solve this problem, the MACRO coding environment of the EES software utilizes the interfacing between the two software. In this way, when the developed model is implemented in MATLAB software, the instruction to run EES software, which includes the water desalination model MED, is issued by the MACRO environment. By doing this, by running the MATLAB software, the EES application is executed, and the problem described is resolved.
To overcome the flaw in the separation of the first, and second laws of thermodynamics, we first obtain the general rule of the lost labor in general. In this section, the overall results will be simple. The potential of a system that only has a heat exchange environment is called its exergy state or thermodynamic access to its dead state. Exergy is the maximum useful work that can be obtained from a material stream or energy: as stated, useful work will be maximized if the process is reversible. Therefore, reversible work with exergy has a relationship. The physical and chemical exergy values form the exergy of material streams can be calculated by equation (3) & (4). The specific chemical exergy for methane can be obtained as equation (5)[48].
The chemical exergy of seawater streams (molar basis) in kJ/kmol is given as follow[50, 51]:
Which is moles number of salt in seawater, and is that of water. Moreover, is the molar chemical potential of salt in seawater in kJ/kmol, and is that of water. The superscript zero indicates the global dead state so that , and . The chemical exergy of seawater streams (mass basis) can be obtained in kJ/kg[50, 51]:
Which is a mass fraction of salt in seawater, and is that of water. Moreover, is a chemical potential of salt in seawater in kJ/kg at restricted dead state condition, and is that of water. The superscript * indicates the restricted dead state so that . The total exergy of a material stream is given as follow[48, 49]:
The exergy rate of the material streams can be determined as follow[48, 49]
The exergy destruction rate and exergetic efficiency of each component can be calculated by equations 10 and 11[48, 49].
The fuel and product exergy rate are two major values that can be defined in each component of the cycle. Table 6 shows the exergy rate of the fuel and product streams in equipment.
Exergoeconomic or thermoeconomic is a branch of engineering that combines exergy analysis with economic principles, and thus provides designers of a system with information that is not available through routine analysis of energy and economic research, but for the design, and operation of an optimally priced system is critical. Therefore, the objectives of exergy control analysis include the separate calculation of the costs of each product produced by the multi-product system, the perception of the process of cost formation, and system flow, the optimization of specific variables in a single component, and the overall optimization of the system. Different methods have been proposed for exergy-cosmetic analysis. In this research, a special cost method for exergy has been used. This cost-based approach to exergy units, exergy efficiency, and auxiliary equations for different components of the thermal system is based. This method involves the identification of exergy flows, the identification of fuel and product for each component of the thermal system, and the use of cost relationships. In Exergy pricing, an expense is assigned to each exergy stream. These exergy currents include the exergy transmitted by the inlets and outlets, by work and by heat. Table 7 shows the purchased cost of equipment.
The cost rate of the equipment can be obtained as equation 9[49].
: the maintenance factor: 1.06[48, 49]. N: the annual operating hours of the system: hours[48, 49]. CRF: the capital recovery factor[48]:
i: interest rate ny: the working years of the system that considered 25 years[48, 49]. the exergoeconomic balance equation for each component in the cycle can be written as follow[48].
The exergy destruction’s cost rate of the equipment is given as follows [48].
The exergoeconomic factor for each component can be calculated as follow[48].
The relative cost difference of the equipment is another parameter that can be obtained as equation 16 [48]:
The exergoenvironmental analysis includes three steps. First, an exergy analysis has been determined for each stream of the cycle, and in the second step the environmental impacts of each component in the process of the manufacturing has been calculated, and then in the third step the exergoenvironmental balance equation has been developed to calculate the environmental impact of each stream in the cycle. The exergoenvironmental balance equation for each component can be written as follow[52].
The exergy destruction’s environmental impact rate of the equipment can be found in equation 14[52].
The exergoenvironmental factor for each component can be obtained as equation 15[52].
The relative environmental impact difference of the equipment are given as follow :[52]
Environmental impact of the equipment multiplying weight, and environmental impact per mass unit of the components:[52]
Which is the environmental impact of the component in pts, and is the weight of the component in tons. is environmental impact per mass unit of the component in pts/ton which is a function of the component’s material, and it can be derived from Eco-indicator 99 knowing the material composition of each component[53]. The weight function of each component is given in table 8.
The weight function of TVC is derived and proposed in this paper using technical data of TVCs in different nominal sizes manufactured by KADANT incorporation. Environmental impact rate of RO in distillate using interpolation data gathered, and can be calculated by equation [54]:
The environmental impact rate of MED in distillate is equal to [54].
In short, the Genetic Algorithm (GA) is a programming technique that uses genetic evolution as a problem-solving paradigm. The problem to be addressed is input, and the solutions are coded according to a pattern called fitness function, and each path Evaluates the candidate solution, most of which are selected at random.Genetic Algorithm (GA) is a computer science search technique for finding optimal solutions and search problems. Genetic algorithms are one of a variety of evolutionary algorithms that are inspired by the science of biologics such as inheritance, mutation, natural selection, and natural selection. The optimization procedure in the genetic algorithm is based on a random-directed procedure. This method is based on the theory of gradual evolution and Darwin's fundamental ideas. In this method, a set of random parameters is randomly generated for several constants called populations, after executing a numerical simulator that represents the standard deviation and Or we fit that set of information to that member of that population. We repeat this procedure for each of the created members, and then call upon the genetic algorithm operators, including fertilization, mutation, and next-generation selection, and this process will continue until the convergence criterion is satisfied. Commonly, three criteria are considered as a stop criterion: - Algorithm execution time
- The number of generations created
- The convergence of error criteria
**Results and discussion**
As stated, the studied cycle included the steam cycle of the Qeshm combined cycle power plant and one water desalination unit. To start the thermal water desalination, a discharge from the line of the LP steam cycle of the power plant has been used. In the following, the reason for using this section is the combined cycle, and then the results of the exergy analysis of this cycle and the effect of discharge on the operation of the power plant are explained. In a power plant, there is a combination of points that can be used as a source of energy in other heating systems, such as hot water sprinklers. These points include the heat dissipated by the outlet of the power plant chimney, the steam outlet from the LP line, and the entrance to the condenser, the discharge line of the LP and HP. Regarding the use of waste heat from the chimney, which is done by adding an auxiliary cycle to the end of the boiler, it should be noted that this mode cannot supply the pressure required for the commissioning of the thermocouple. However, it is suitable for use in other types of water Thermal desalination unit without Thermo compressor. In the case of the steam outlet from the LP line, and the use of the first stage of the desalination system instead of the condenser, it should be noted that this steam not only does not have the ability to supply the pressure required for the commissioning of the thermocouple compressor, but because of its low temperature, It is also not used in other types of thermal desalination. Concerning the withdrawal of the HP line due to the high steam pressure at this stage and that this pressure is outside the pressure range of the thermocouple compressors, the idea of using high-pressure turbine steam line steam for use in MED-TVC It is also excluded. Here, the idea of using an auxiliary burner in a power plant boiler and supplying a desirable water supply can be made into mind. Nevertheless, because of the increased energy consumption in this case and the goal of recycling and reducing energy consumption in the survey. The project for the production of electricity, and water Qeshm, to save fossil fuels and increase the efficiency of gas power plants, was exploited with a capacity of 50 megawatts of electricity and 18 thousand cubic meters of Freshwater. The thermodynamic properties of the cycle include: mass flow, temperature, and pressure are presented in table 11. The exergy rate of each stream is indicated in this table, and the cost rate and environmental are determined.
The stream No.4, which is the output stream of the combustion chamber, has the highest exergy rate among all cyclic flows. This flow is about 90 megawatts of exergy. In addition, the flow of the outlet from the combustion chamber has the highest cost rate in the cyclic flows. This stream costs around $ 3,548.5 per hour per cycle. It also has the highest altitudinal rate throughout the entire cycle. In this process, the rate of annoyance is about 1471 mpts per second. The reason for the high rate of exergy in this flow is the high temperature, and pressure of the exhaust stream from the combustion chamber. Also due to the use of fossil fuels in the combustion chamber, the cost, and degree of contamination of this stream is high. Nevertheless, after the flow of the outlet from the combustion chamber, the fuel flow into it has the highest exergy rate. It has an exergy content of about 73 megawatts. The cost of the fuel flow is about $ 1703 per hour, and its pollution is about 753 mpts per hour. The compressor consumes 62% of the power output by the gas turbine. The amount of heat exchanged in each of the heat exchangers through MATLAB coding, and thermoflow simulation is shown in Table 12. Also, the amount of error between computer code, and Thermoflex simulation has been reported. The performance ratio of each sweetener is another important parameter. This amount for MEDTVC is about 8.7. This value represents the proportion of sweet water produced to steam consumption. This amount for RO is 0.5. The exergy destruction rate in each component has been presented in the figure 2.
According to Fig. 2, the highest rate of exergy degradation is related to the combustion chamber, which accounts for about 45.5% of the total exergy destruction of the cycle. The combustion chamber has about 19.5 megawatts of exergy destruction. The process heat exchanger is the next device that has the highest rate of exergy destruction. This equipment has about 6.14 megawatts of exergy destruction, which is about 15% of the total exergy destruction of the cycle. The exergy destruction of the air compressor is 13%, and the gas turbine has 8% of total exergy destruction. The MED unit also has a 7% destruction of the exergy cycle. The ever-increasing demand for water, and services resulting from population growth, and rising standards of living, and health, on the one hand, and the limitation of water resources and droughts and climate change, on the other hand, is the view of planners and water experts from unconventional waters (sewage, wastewater, and saline water). Also, the disposal of industrial, and urban wastewater, and the penetration of existing contaminations into surface water, and groundwater resources is a major concern in many countries, including Iran. Sewage treatment and its application in various uses negatively affects the release of wastewater to the environment, and the health of human societies. Based on this, in this paper, the methodology of economic and environmental assessment of sweet water production from Persian Gulf and the economic and environmental assessment of this project has been addressed. The exergoenvironmental and exergoeconomic analysis results are presented in table 13.
The highest rate of purchase is related to the air compressor, and then desalination unit also have a high cost rate. The cost of exergy destruction in the combustion chamber has the highest rate, and it costs $ 630 per hour. The cost of exergy destruction in the combustion chamber is approximately 3 times the air compressor, and 5 times the gas turbine. Similarly, the rate of emissions associated with exergy destruction in the combustion chamber has the highest rate. Genetic algorithms are better because of their strength and durability than other methods based on artificial intelligence. Unlike older artificial intelligence systems, the genetic algorithm is not quickly interrupted by slight changes in input values or by significant amounts of noise in the system. Also, in the search for a large state space, a multimodal state space, or a multidimensional procedure, the use of genetic algorithms has many advantages over conventional search techniques in other optimization techniques such as linear programming, random search, or the first search methods have depth, first level or praxis. The objective functions are produced by Genetic programming and the functions are presented in Table 13. Figure 3shows the optimal pareto front solutions for twoObjective Functions (OFs) (exergetic efficiency and total exrgetic costs). In addition, Figure 4 and 5 determine pareto front optimal solutions for total exergeticcost vs exergeticenvironmental impacts OFs and exergeticefficiency vs exergeticenvironmental impactsOFs respectively.
Table 14 and 15 are indicated the optimized variables of the objective functions and decision variables. As shown in the results, the overall exergetic efficiency of plant has been improved by 27.74%. Also, the exergeticcost of plant has been reduced by 0.93 $/min and exergoenvironmental impacts has been decreased by 0.85 pts/min. Sensitivity analysis for objective functions has been performed based on variation of fuel LHV, ambient temperature, interest rate and exergy cost of fuel. The results of sensitivity analysis related to variation of fuel LHV, ambient temperature, interest rate, exergy cost of fuel have been demonstrated in Figure Fig.6-Fig.9 respectively.
**Conclusion**
In this study, energetic, exergetic, exergeoeconomic and exergoenvironmental analysis and optimization of Qeshm MED-TVC cogeneration plant based on 25 MW, MAPNA Gas Turbine prime mover have been considered. In this regard, the computer program has been developed. Also, the integration of the RO desalination system has been investigated. MOGA optimization of existing plant-based on overall exergetic efficiency, total exergetic costs and total exergoenvironmental impacts have been done. The results indicate the optimum scenario has a good performance in view of exergetic, exergoeconomic and exergoenvironment. The optimum plant overall exergeticefficiency hasbeen increased by 27.78%, and total exergetic cost and total exergoenvironmental impacts have been decreased by 0.93% and by 0.89%. In the future research, the advanced exergetic, exergoeconomic and exergoenvironmental analysis can be done to better show the performance of system in the base and optimum cases precisely. In addition, other recently optimization algorithms can be examined and evaluated. Finally, the use of renewable energy to improve the plant performance can be studied.
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