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Journal articles on the topic 'Exergy cost'

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Published: 1 April 2023

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1

Tsatsaronis, George, and Michael J. Moran. "Exergy-aided cost minimization." Energy Conversion and Management 38, no. 15-17 (October 1997): 1535–42. http://dx.doi.org/10.1016/s0196-8904(96)00215-4.

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2

Yazawa, Kazuaki, and Ali Shakouri. "D135 Exergy Analysis of Cost Effective Thermoelectric Topping Cycles." Proceedings of the National Symposium on Power and Energy Systems 2014.19 (2014): 137–38. http://dx.doi.org/10.1299/jsmepes.2014.19.137.

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3

Torres, César, and Antonio Valero. "The Exergy Cost Theory Revisited." Energies 14, no. 6 (March 13, 2021): 1594. http://dx.doi.org/10.3390/en14061594.

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This paper reviews the fundamentals of the Exergy Cost Theory, an energy cost accounting methodology to evaluate the physical costs of products of energy systems and their associated waste. Besides, a mathematical and computationally approach is presented, which will allow the practitioner to carry out studies on production systems regardless of their structural complexity. The exergy cost theory was proposed in 1986 by Valero et al. in their “General theory of exergy savings”. It has been recognized as a powerful tool in the analysis of energy systems and has been applied to the evaluation of energy saving alternatives, local optimisation, thermoeconomic diagnosis, or industrial symbiosis. The waste cost formation process is presented from a thermodynamic perspective rather than the economist’s approach. It is proposed to consider waste as external irreversibilities occurring in plant processes. A new concept, called irreversibility carrier, is introduced, which will allow the identification of the origin, transfer, partial recovery, and disposal of waste.
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4

Rosa, Rui N., and Diogo R. N. Rosa. "Exergy cost of mineral resources." International Journal of Exergy 5, no. 5/6 (2008): 532. http://dx.doi.org/10.1504/ijex.2008.020824.

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5

Ptasinski, Krzysztof J. "Exergy: Production, Cost and Renewability." Energy 55 (June 2013): 1209. http://dx.doi.org/10.1016/j.energy.2013.03.044.

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6

Valencia Ochoa, Guillermo, Jhan Piero Rojas, and Jorge Duarte Forero. "Advance Exergo-Economic Analysis of a Waste Heat Recovery System Using ORC for a Bottoming Natural Gas Engine." Energies 13, no. 1 (January 5, 2020): 267. http://dx.doi.org/10.3390/en13010267.

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This manuscript presents an advanced exergo-economic analysis of a waste heat recovery system based on the organic Rankine cycle from the exhaust gases of an internal combustion engine. Different operating conditions were established in order to find the exergy destroyed values in the components and the desegregation of them, as well as the rate of fuel exergy, product exergy, and loss exergy. The component with the highest exergy destroyed values was heat exchanger 1, which is a shell and tube equipment with the highest mean temperature difference in the thermal cycle. However, the values of the fuel cost rate (47.85 USD/GJ) and the product cost rate (197.65 USD/GJ) revealed the organic fluid pump (pump 2) as the device with the main thermo-economic opportunity of improvement, with an exergo-economic factor greater than 91%. In addition, the component with the highest investment costs was the heat exchanger 1 with a value of 2.769 USD/h, which means advanced exergo-economic analysis is a powerful method to identify the correct allocation of the irreversibility and highest cost, and the real potential for improvement is not linked to the interaction between components but to the same component being studied.
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7

Shamoushaki, Moein, Mehdi Aliehyaei, and Farhad Taghizadeh-Hesary. "Energy, Exergy, Exergoeconomic, and Exergoenvironmental Assessment of Flash-Binary Geothermal Combined Cooling, Heating and Power Cycle." Energies 14, no. 15 (July 23, 2021): 4464. http://dx.doi.org/10.3390/en14154464.

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This research presents the energy, exergy, economic, and environmental assessment, and multi-objective optimization of a flash-binary geothermal CCHP cycle. A sensitivity analysis of production well inlet temperature and cooling to power flow ratio on exergetic, economic, and environmental parameters was conducted. Furthermore, the effects of the inflation rate and plant working hours on economic parameters were investigated. Results showed that increasing the production well inlet temperature harms exergy efficiency and exergetic performance criteria and results in a gain in exergo-environmental impact index and heating capacity. In addition, the total plant cost increased by raising the production well temperature. Furthermore, increasing the cooling to power flow ratio caused a reduction in exergy efficiency, exergetic performance criteria, and produced net power and an enhancement in exergy destruction, cooling capacity, and total plant cost. The exergy efficiency and total cost rate in the base case were 58% and 0.1764, respectively. Optimization results showed that at the selected optimum point, exergy efficiency was 4.5% higher, and the total cost rate was 10.3% lower than the base case. Levelized cost of energy and the pay-back period at the optimum point was obtained as 6.22 c$/kWh, 3.43 years, which were 5.14% and 6.7% lower than the base case.
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8

Valero, Alicia, Antonio Valero, and Adriana Domínguez. "Exergy Replacement Cost of Mineral Resources." Journal of Environmental Accounting and Management 1, no. 2 (June 2013): 147–58. http://dx.doi.org/10.5890/jeam.2013.05.004.

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9

Tsatsaronis, G., L. Lin, and J. Pisa. "Exergy Costing in Exergoeconomics." Journal of Energy Resources Technology 115, no. 1 (March 1, 1993): 9–16. http://dx.doi.org/10.1115/1.2905974.

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Existing methods of exergoeconomic analysis and optimization of energy systems operate with single average or marginal cost values per exergy unit for each material stream in the system being considered. These costs do not contain detailed information on (a) how much exergy, and (b) at what cost each exergy unit was supplied to the stream in the upstream processes. The cost of supplying exergy, however, might vary significantly from one process step to the other. Knowledge of the exergy addition and the corresponding cost at each previous step can be used to improve the costing process. This paper presents a new approach to exergy costing in exergoeconomics. The monetary flow rate associated with the thermal, mechanical and chemical exergy of a material stream at a given state is calculated by considering the complete previous history of supplying and removing units of the corresponding exergy form to and from the stream being considered. When exergy is supplied to a stream, the cost of adding each exergy unit to the stream is calculated using the cost of product exergy unit for the process or device in which the exergy addition occurs. When the stream being considered supplies exergy to another exergy carrier, the last-in-first-out (LIFO) principle of accounting is used for the spent exergy units to calculate the cost of exergy supply to the carrier. The new approach eliminates the need for auxiliary assumptions in the exergoeconomic analysis of energy systems and improves the fairness of the costing process by taking a closer look at both the cost-formation and the monetary-value-use processes. This closer look mainly includes the simultaneous consideration of the exergy and the corresponding monetary values added to or removed from a material stream in each process step. In general, the analysis becomes more complex when the new approach is used instead of the previous exergoeconomic methods. The benefits of using the new approach, however, significantly outweigh the increased efforts. The new approach, combined with some other recent developments, makes exergoeconomics an objective methodology for analyzing and optimizing energy systems.
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Wang, Jixuan, Wensheng Liu, Xin Meng, Xiaozhen Liu, Yanfeng Gao, Zuodong Yu, Yakai Bai, and Xin Yang. "Study on the Coupling Effect of a Solar-Coal Unit Thermodynamic System with Carbon Capture." Energies 13, no. 18 (September 14, 2020): 4779. http://dx.doi.org/10.3390/en13184779.

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Based on the structural theory of thermo-economics, a 600 MW unit was taken as an example. An integration system which uses fuel gas heat and solar energy as a heat source for post-combustion carbon capture was proposed. The physical structure sketch and productive structure sketch were drawn and a thermo-economics model and cost model based on the definition of fuel-product were established. The production relation between units was analyzed, and the composition and distribution of the exergy cost and thermo-economic cost of each unit were studied. Additionally, the influence of the fuel price and equipment investment cost of the thermo-economic cost for each product was studied. The results showed that the main factors affecting the unit cost are the fuel exergy cost, component exergy efficiency, and irreversible exergy cost of each unit, and the main factors affecting the thermo-economics cost are the specific irreversible exergy cost and investment exergy cost. The main factors affecting the thermal economics of solar energy collectors and low-pressure economizers are the invested exergy cost, negentropy exergy cost, and irreversible exergy cost of each unit.
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11

Khedr, Sobhy, Melchiorre Casisi, and Mauro Reini. "The Thermoeconomic Environment Cost Indicator (iex-TEE) as a One-Dimensional Measure of Resource Sustainability." Energies 15, no. 6 (March 19, 2022): 2260. http://dx.doi.org/10.3390/en15062260.

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This paper presents a conceptual development of sustainability evaluation, through an exergy-based indicator, by using the new concept of the Thermoeconomic Environment (TEE). The exergy-based accounting methods here considered as a background are Extended Exergy Accounting (EEA), which can be used to quantify the exergy cost of externalities like labor, monetary inputs, and pollutants, and Cumulative Exergy Consumption (CExC), which can be used to quantify the consumption of primary resources embodied in a final product or service. The new concept of bioresource stock replacement cost is presented, highlighting how the framework of the TEE offers an option for evaluating the exergy cost of products of biological systems. This sustainability indicator is defined based on the exergy cost of all resources directly and indirectly consumed by the system, the equivalent exergy cost of all externalities implied in the production process and the exergy cost of the final product.
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12

Ledari, Masoomeh Bararzadeh, Yadollah Saboohi, Antonio Valero, and Sara Azamian. "Exergy cost analysis of soil-plant system." International Journal of Exergy 38, no. 3 (2022): 293. http://dx.doi.org/10.1504/ijex.2022.124174.

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13

Bararzadeh Ledari, Masoomeh, Yadollah Saboohi, Antonio Valero, and Sara Azamian. "Exergy cost analysis of soil-plant system." International Journal of Exergy 38, no. 3 (2022): 293. http://dx.doi.org/10.1504/ijex.2022.10048872.

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14

Nixon, J. D., and P. A. Davies. "Cost-exergy optimisation of linear Fresnel reflectors." Solar Energy 86, no. 1 (January 2012): 147–56. http://dx.doi.org/10.1016/j.solener.2011.09.024.

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15

Muhammad Penta Helios, Achmad Maswan, Riki Jaka Komara, Himawan Sutriyanto, Bhakti Nuryadin, and Ade Andini. "Energy, Exergy, and Externalities Cost Rate Analysis of 300 MW Coal-Fired Power Plant: A Case Study." Majalah Ilmiah Pengkajian Industri 16, no. 3 (December 29, 2022): 103–13. http://dx.doi.org/10.29122/mipi.v16i3.5405.

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Three types of analysis conducted at one of Thailand's coal-fired power plants were reported in this paper. The analyses consisting of energy, exergy, and externalities cost rate analysis are aimed to analyse the largest energy loss and exergy destruction that occurs in the system, to assess the contribution of Energy externalities cost rate based on fuel price, and to determine potential cost saving. Energy loss at the condenser was the highest among major units of the Thai power plants, which contributed around 49.11% at full load condition and was followed by a boiler, turbine, etc. Furthermore, the boiler was identified as the highest exergy destruction producer, with around 57.73% of total exergy input into the system, followed by turbines, heaters, etc. Moreover, the energy and exergy efficiency of Thai's power plant was calculated to be around 35.60% and 31.76%, respectively. The highest externalities cost rate due to energy loss occurred in the condenser was about 0.56 $/s, whereas the highest externalities cost rate due to exergy destruction identified in the boiler was about 0.67 $/s. By improving boiler and turbine components, Thai's PP has a potential cost saving of around 21.2 million $/year, reducing 88.44% of the externalities cost of exergy destruction. Keywords: Energy loss, Exergy destruction, Externalities cost rate, Potential saving cost.
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16

Oyedepo, S. O., R. O. Fagbenle, S. S. Adefila, and Md Mahbub Alam. "Exergoeconomic analysis and performance assessment of selected gas turbine power plants." World Journal of Engineering 12, no. 3 (August 1, 2015): 283–300. http://dx.doi.org/10.1260/1708-5284.12.3.283.

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In this study, exergoeconomic analysis and performance evaluation of selected gas turbine power plants in Nigeria were carried out. The study was conducted using operating data obtained from the power plants to determine the exergy efficiency, exergy destruction, unit cost of electricity and cost of exergy destruction of the major components of a gas turbine engine in the selected power plants. The results of exergy analysis confirmed that the combustion chamber is the most exergy destructive component compared to other cycle components as expected. The total efficiency defects and overall exergetic efficiency of the selected power plants vary from 38.64 to 69.33% and 15.66 to 30.72% respectively. The exergy analysis further shows that the exergy improvement potential of the selected plants varies from 54.04 MW to 159.88 MW. The component with the highest exergy improvement potential is the combustion chamber and its value varies from 30.21 MW to 88.86 MW. The results of exergoeconomic analysis show that the combustion chamber has the greatest cost of exergy destruction compared to other components. Increasing the gas turbine inlet temperature (GTIT), both the exergy destruction and the cost of exergy destruction of this component were found to decrease. The results of this study revealed that an increase in the GTIT of about 200 K can lead to a reduction of about 29% in the cost of exergy destruction. From exergy costing analysis, the unit cost of electricity produced in the selected power plants varies from cents 1.99 /kWh (N3.16 /kWh) to cents 5.65 /kWh (N8.98 /kWh).
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17

Liu, Sha, and Pei Hong Wang. "Calculation Model of Exergy Cost Based on Thermoeconomics Structure Theory and Thermoeconomics Accounting Mode." Applied Mechanics and Materials 313-314 (March 2013): 1148–52. http://dx.doi.org/10.4028/www.scientific.net/amm.313-314.1148.

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Thermoeconomics combines the thermodynamic analysis and economics evaluation, and simultaneously considers the thermodynamics and economics effect of the process of energy conversion in power plant. It becomes the focus of research. This paper mainly discusses the establishment method of the exergy cost equation in thermoeconomics structure theory, at the same time this method also combines with thermoeconomics accounting theory. Through the research, this paper presents a clear, simple, utility exergy cost equation established method. Compared with the chain differential principle, this method has the advantages of a simple form of expression and faster calculation speed. The method is applied to an actual 600MW power plant, established exergy cost equation and obtained the exergy cost for each component.The exergy cost concept is used to evaluate the production performance of the major equipment, to find the reason of production cost growing and direct the thermal power systems exergy optimization.
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18

Marques, Adriano da S., Monica Carvalho, Álvaro A. V. Ochoa, Ronelly J. Souza, and Carlos A. C. dos Santos. "Exergoeconomic Assessment of a Compact Electricity-Cooling Cogeneration Unit." Energies 13, no. 20 (October 16, 2020): 5417. http://dx.doi.org/10.3390/en13205417.

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This study applies the SPecific Exergy COsting (SPECO) methodology for the exergoeconomic assessment of a compact electricity-cooling cogeneration system. The system utilizes the exhaust gases from a 126 hp Otto-cycle internal combustion engine (ICE) to drive a 5 RT ammonia–water absorption refrigeration unit. Exergy destruction is higher in the ICE (67.88%), followed by the steam generator (14.46%). Considering the cost of destroyed exergy plus total cost rate of equipment, the highest values are found in the ICE, followed by the steam generator. Analysis of relative cost differences and exergoeconomic factors indicate that improvements should focus on the steam generator, evaporator, and absorber. The cost rate of the fuel consumed by the combustion engine is 12.84 USD/h, at a specific exergy cost of 25.76 USD/GJ. The engine produces power at a cost rate of 10.52 USD/h and specific exergy cost of 64.14 USD/GJ. Cooling refers to the chilled water from the evaporator at a cost rate of 0.85 USD/h and specific exergy cost of 84.74 USD/GJ. This study expands the knowledge base regarding the exergoeconomic assessment of compact combined cooling and power systems.
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19

Basta, Giuseppe, Nicoletta Meloni, Francesco Poli, Lorenzo Talluri, and Giampaolo Manfrida. "Energy, Exergy and Exergo-Economic Analysis of an OTEC Power Plant Utilizing Kalina Cycle." Global Journal of Energy Technology Research Updates 8 (December 28, 2021): 1–18. http://dx.doi.org/10.15377/2409-5818.2021.08.1.

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This study aims to analyse an Ocean Thermal Energy Conversion (OTEC) system through the use of a Kalina Cycle (KC), having a water-ammonia mixture as a working fluid. KC represents a technology capable of exploiting the thermal gap of ocean water. This system was then compared with OTEC systems, which exploit ammonia, R134A and butane-pentane mixture as working fluid. The comparison was carried on through energy analysis, exergetic analysis, and exergo-economic analysis using the EES (Engineering Equation Solver) software. For each case study, cost rates and auxiliary equations were evaluated for all components and the mass flow rate and unit exergy cost for each stream. The results showed that the KC with water-ammonia as working fluid achieves the best exergo-economic performance among the examined cycles. The cost of electricity produced through KC using water - ammonia mixture was found to be 26,66 c€/kWh. The thermal efficiency and the exergetic efficiency were calculated and the withdrawal depth of ocean water was considered. The efficiencies resulted to be 3.68% for the thermal efficiency and 95.96% for the exergetic efficiency.
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20

Sciubba, Enrico. "Exergy-based ecological indicators: From Thermo-Economics to cumulative exergy consumption to Thermo-Ecological Cost and Extended Exergy Accounting." Energy 168 (February 2019): 462–76. http://dx.doi.org/10.1016/j.energy.2018.11.101.

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21

Li, Peng, Baokuan Li, Zhongqiu Liu, and Wenjie Rong. "Evaluation and analysis of exergoeconomic performance for the calcination process of green petroleum coke in vertical shaft kiln." Thermal Science, no. 00 (2021): 294. http://dx.doi.org/10.2298/tsci210609294l.

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The main objective of this paper is to establish a mathematical framework to analyze the complex thermal economic performance of the calcination process. To find the factors affecting exergy efficiency loss, different exergy destruction is investigated in detail. Furthermore, the exergy flow cost model for exergy cost saving has also been developed. The results show that the vertical shaft furnace is a self-sufficiency equipment without additional fuel required, but the overall exergy destruction accounts for 54.11% of the total exergy input. In addition, the energy efficiency of the waste heat recovery boiler and thermal deaerator are 83.52% and 96.40%, whereas the exergy efficiency of the two equipment are 65.98% and 94.27%. Furthermore, the import exergy flow cost of vertical shaft furnace, waste heat recovery boiler and thermal deaerator are 366.5197 RMB/MJ, 0.1426 RMB/MJ and 0.0020RMB/MJ, respectively. Based on the result, several suggestions were proposed to improve the exergoeconomic performance. Assessing the performance of suggested improvements, the total exergy destruction of vertical shaft furnace is reduced to 134.34 GJ/h and the exergy efficiency of waste heat recovery boiler is raised up to 66.02%. Moreover, the import exergy flow cost of the three different equipment is reduced to 0.0329 RMB/MJ, 0.1304 RMB/MJ and 0.0002 RMB/MJ, respectively.
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22

Nasruddin, Septian Khairul Masdi, and Arief Surachman. "Exergy Analysis and Exergoeconomic Optimization with Multiobjective Method of Unit 4 Kamojang Geothermal Power Plant." Applied Mechanics and Materials 819 (January 2016): 523–29. http://dx.doi.org/10.4028/www.scientific.net/amm.819.523.

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This study presents four analysis at unit 4 Kamojang geothermal power plant are exergy analysis at current condition, exergy efficiency optimization, economic optimization, and exergoeconomic optimization with wellhead valve pressure as a variable. Calculations are conducted by using the MATLAB. Thermodynamics characteristic of geothermal fluid assumed as water characteristic which get from REFPROP. Wellhead pressure operational condition 10 bar has exergy efficiency 31.91%. Exergy efficiency optimization has wellhead valve pressure 5.06 bar, exergy efficiency 47.3%, and system cost US$ 3,957,100. Economic optimization has well pressure 11 bar, exergy efficiency 22.13%, and system cost US$ 2,242,200. Exergoeconomic optimization has 15 optimum condition. Exergoeconomic optimization aims to analyze the optimum wellhead valve pressure for maximum exergy efficiency and minimum cost of power plant system.
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23

Xiang, Jing Yan, Jun Zhao, Xi Kui Wang, and Bao Zhu Zhao. "Dynamic Exergetic Cost Analysis of a Space Heating System." Advanced Materials Research 354-355 (October 2011): 722–25. http://dx.doi.org/10.4028/www.scientific.net/amr.354-355.722.

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The design of heating systems with groundwater source heat pumps (GWHP) is very important for reducing their power consumption. For better design, reasonable analysis of the systems is necessary. In this paper, a dynamic exergy and exergetic cost analysis of a heating system with GWHP is performed in a whole heating season by the use of structural theory of thermoeconomics and the software of TRNSYS. The relative exergy destruction of every component and the exergetic cost of the final product of the system are obtained. The results show that the heat pump has the largest relative exergy destruction under all the working conditions. The terminal unit component has the second largest relative exergy destruction at conditions above 10% load. However, at 10% load, well water transportation component has the second largest relative exergy destruction. The unit exergetic cost of the system final product during the whole heating season is 8.51W/W, similar to the result at 75% load.
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24

Aras, Haydar, and Ozgur Balli. "Exergoeconomic Analysis of a Combined Heat and Power System with the Micro Gas Turbine (MGTCHP)." Energy Exploration & Exploitation 26, no. 1 (February 2008): 53–70. http://dx.doi.org/10.1260/014459808784305824.

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This paper presents the results of exergy and exergoeconomic analyses applied to a combined heat and power system with micro-gas turbine (MGTCHP). Quantative balances of the exergy and exergy cost for each component and for the whole system are carefully considered, while exergy consumption and cost generation within the system are determined. The exergy analysis indicates that the exergetic efficiency of the MGTCHP system is 35.80% with 123 kW (as 99.15 kW-electrical power and 24.46 kW-hot water@363.15 K). On the other hand, the exergoeconomic analysis results show that the unit exergy cost of electrical power and hot water produced by the MGTCHP system are accounted as 26.808 €(GW)−1 and 7.737 €(GW)−1, respectively.
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Yazdi, Behnam, Behdad Yazdi, Mehdi Ehyaei, and Abolfazl Ahmadi. "Optimization of micro combined heat and power gas turbine by genetic algorithm." Thermal Science 19, no. 1 (2015): 207–18. http://dx.doi.org/10.2298/tsci121218141y.

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In this paper, a comprehensive thermodynamic modeling and multi-objective optimization of a micro turbine cycle in combined heat and power generation, which provides 100KW of electric power. This CHP System is composed of air compressor, combustion chamber (CC), Air Preheater, Gas Turbine (GT) and a Heat Recovery Heat Exchanger. In this paper, at the first stage, the each part of the micro turbine cycle is modeled using thermodynamic laws. Next, with using the energetic and exergetic concepts and applying economic and environmental functions, the multi-objectives optimization of micro turbine in combined heat and power generation is performed. The design parameters of this cycle are compressor pressure ratio (rAC), compressor isentropic efficiency (?AC), GT isentropic efficiency (?GT), CC inlet temperature (T3), and turbine inlet temperature (T4). In the multi-objective optimization three objective functions, including CHP exergy efficiency, total cost rate of the system products, and CO2 emission of the whole plant, are considered. Theexergoenvironmental objective function is minimized whereas power plant exergy efficiency is maximized usinga Genetic algorithm. To have a good insight into this study, a sensitivity analysis of the result to the fuel cost is performed. The results show that at the lower exergetic efficiency, in which the weight of exergo-environmental objective is higher, the sensitivity of the optimal solutions to the fuel cost is much higher than the location of the Pareto Frontier with the lower weight of exergo-environmental objective. In addition, with increasing exergy efficiency, the purchase cost of equipment in the plant is increased as the cost rate of the plant increases.
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26

Gonçalves, L. P., and F. R. P. Arrieta. "AN EXERGY COST ANALYSIS OF A COGENERATION PLANT." Revista de Engenharia Térmica 9, no. 1-2 (December 31, 2010): 28. http://dx.doi.org/10.5380/reterm.v9i1-2.61927.

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The exergy analysis, including the calculation of the unit exergetic cost of all flows of the cogeneration plant, was the main purpose of the thermoeconomic analysis of the STAG (STeam And Gas) combined cycle CHP (Combined Heat and Power) plant. The combined cycle cogeneration plant is composed of a GE10 gas turbine (11250 kW) coupled with a HRSG (Heat Recovery Steam Generator) and a condensing extraction steam turbine. The GateCycleTM Software was used for the modeling and simulation of the combined cycle CHP plant thermal scheme, and calculation of the thermodynamic properties of each flow (Mass Flow, Pressure, Temperature, Enthalpy). The entropy values for water and steam were obtained from the Steam Tab software while the entropy and exergy of the exhaust gases were calculated as instructed by. For the calculation of the unit exergetic cost was used the neguentropy and Structural Theory of Thermoeconomic. The GateCycleTM calculations results were exported to an Excel sheet to carry out the exergy analysis and the unit exergetic cost calculations with the thermoeconomic model that was created for matrix inversion solution. Several simulations were performed varying separately five important parameters: the Steam turbine exhaust pressure, the evaporator pinch point temperature, the steam turbine inlet temperature, Rankine cycle operating pressure and the stack gas temperature to determine their impact in the recovery cycle heat exchangers transfer area, power generation and unit exergetic cost.
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27

Himsworth, J. R. "Exergy Overhead: The Cost of Operating a Process." International Journal of Mechanical Engineering Education 19, no. 1 (January 1991): 29–31. http://dx.doi.org/10.1177/030641909101900105.

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28

WANG, Songping. "Transfer equation of exergy cost and its application." Chinese Science Bulletin 48, no. 7 (2003): 619. http://dx.doi.org/10.1360/03tb9131.

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29

Wang, Songping, Qinglin Chen, Qinghua Yin, and Ben Hua. "Transfer equation of exergy cost and its application." Science Bulletin 48, no. 7 (April 2003): 619–22. http://dx.doi.org/10.1007/bf03325640.

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30

Acevedo, Luis, Sergio Usón, and Javier Uche. "Local exergy cost analysis of microwave heating systems." Energy 80 (February 2015): 437–51. http://dx.doi.org/10.1016/j.energy.2014.11.085.

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31

Tumen, Ozdil, and Atakan Tantekin. "Exergoeconomic analysis of a fluidized bed coal combustion steam power plant." Thermal Science 21, no. 5 (2017): 1975–84. http://dx.doi.org/10.2298/tsci151210056t.

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In this study, extensive exergoeconomic analysis is performed for a 6.5 MW steam power plant using the data obtained from running system. The role and impact of the each system component on the first and second law efficiencies are analyzed to understand the individual performance of sub-components. Moreover, the quantitative exergy cost balance for each component is considered to point out the exergoeconomic performance. The analysis shows that the largest irreversibility occurs in the fluidized bed coal combustion (FBCC), about 93% of the overall system irreversibility. Furthermore, it is followed by heat recovery steam generator and economizer with 3% and 1%, respectively. In this study, the capital investment cost, operating and maintenance costs and total cost of FBCC steam plant are calculated as 6.30, 5.35, and 11.65 US$ per hour, respectively. The unit exergy cost and fuel exergy cost, which enter the FBCC steam plant, are found as 3.33 US$/GJ and 112.44 US$/h, respectively. The unit exergy cost and exergy cost of the steam which is produced in heat recovery steam generator are calculated as 16.59 US$/GJ and 91.87 US$ per hour, respectively. This study emphasizes the importance of the exergoeconomic analysis based on the results obtained from the exergy analysis.
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Oyedepo, Sunday Olayinka, Richard Olayiwola Fagbenle, Samuel Sunday Adefila, and Md Mahbub Alam. "Exergoenvironomic modelling and performance assessment of selected gas turbine power plants." World Journal of Engineering 13, no. 2 (April 8, 2016): 149–62. http://dx.doi.org/10.1108/wje-04-2016-020.

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Purpose This study aims to use an environomics method to assess the environmental impacts of selected gas turbine power plants in Nigeria. Design/methodology/approach In this study, exergoenvironomic analysis has been carried out to investigate the environmental impact of selected gas turbine power plants in Nigeria from an exergetic point of view. Findings The exergy analysis reveals that the combustion chamber is the most exergy destructive component compared to other cycle components. The exergy destruction of this component can be reduced by increasing gas turbine inlet temperature (GTIT). The results of the study show that thermodynamic inefficiency is responsible for the environmental impact associated with gas turbine components. The study further shows that CO2 emissions and cost of environmental impact decrease with increasing GTIT. Originality/value The exergo-environomic parameters computed in this study are CO2 emission in kg per MWh of electricity generated, depletion number, sustainability index, cost flow rate of environmental impacts (Ċenv) in $/h and total cost rates of products (ĊTot) in $/hr. For the period considered, the CO2 emissions for the selected plants vary from 100.18 to 408.78 kgCO2/MWhm, while cost flow rate of environmental impacts varies from $40.18 /h to $276.97 /h and the total cost rates of products vary from $2935.69/h to $12,232.84/h. The depletion number and sustainability index vary from 0.69 to 0.84 and 1.20 to 1.44, respectively.
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Lee, Sang Hyun, Dong-Ha Lim, and Kyungtae Park. "Optimization and Economic Analysis for Small-Scale Movable LNG Liquefaction Process with Leakage Considerations." Applied Sciences 10, no. 15 (August 4, 2020): 5391. http://dx.doi.org/10.3390/app10155391.

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In this study, exergy and economic analysis were conducted to gain insight on small-scale movable LNG liquefaction considering leakage. Optimization and comparison were performed to demonstrate the quantitative results of single mixed refrigerant, dual nitrogen expansion, and the propane pre-cooling self-refrigeration processes. For the optimization, exergy efficiency was used as the objective function; the results showed that exergy efficiencies are 38.85%, 19.96%, and 13.65%, for single mixed refrigerant, dual nitrogen expansion, and propane pre-cooling self-refrigeration, respectively. Further, the cost analysis showed that the product cost of each process is 4002.3 USD/tpa, 5490.2 USD/tpa, and 9608.5 USD/tpa. A sensitivity analysis was conducted to determine parameters that affect exergy and cost. The SMR process is the most competitive in terms of exergy efficiency, product cost, and operability, without considering makeup facilities.
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Ochoa, Guillermo Valencia, Carlos Acevedo Peñaloza, and Jhan Piero Rojas. "Thermoeconomic Modelling and Parametric Study of a Simple ORC for the Recovery of Waste Heat in a 2 MW Gas Engine under Different Working Fluids." Applied Sciences 9, no. 21 (October 25, 2019): 4526. http://dx.doi.org/10.3390/app9214526.

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This paper presents a thermo-economic analysis of a simple organic Rankine cycle (SORC) as a waste heat recovery (WHR) systems of a 2 MW stationary gas engine evaluating different working fluids. Initially, a systematic methodology was implemented to select three organic fluids according to environmental and safety criteria, as well as critical system operational conditions. Then, thermodynamic, exergy, and exergo-economic models of the system were developed under certain defined considerations, and a set of parametric studies are presented considering key variables of the system such as pump efficiency, turbine efficiency, pinch point condenser, and evaporator. The results show the influence of these variables on the combined power of the system (gas engine plus ORC), ORC exergetic efficiency, specific fuel consumption (∆BSFC), and exergo indicators such as the payback period (PBP), levelized cost of energy (LCOE), and the specific investment cost (SIC). The results revealed that heat transfer equipment had the highest exergy destruction cost rates representing 81.25% of the total system cost. On the other hand, sensitivity analyses showed that acetone presented better energetic and exergetic performance when the efficiency of the turbine, evaporator, and condenser pinch point was increased. However, toluene was the fluid with the best results when pump efficiency was increased. In terms of the cost of exergy destroyed by equipment, the results revealed that acetone was the working fluid that positively impacted cost reduction when pump efficiency was improved; and toluene, when turbine efficiency was increased. Finally, the evaporator and condenser pinch point increased all the economic indicators of the system. In this sense, the working fluid with the best performance in economic terms was acetone, when the efficiency of the turbine, pinch condenser, and pinch evaporator was enhanced.
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Braimah, M. N., A. N. Anozie, and R. O. Braimah. "Optimizing Medical Air Production Using Exergy and Process Cost Analysis." Journal of Environmental Science and Engineering Technology 5, no. 1 (February 27, 2017): 16–22. http://dx.doi.org/10.12974/2311-8741.2017.05.01.3.

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This work compared one new design of Air separation using Linde process for medical air production with existing plant using exergy and process cost analyses. Hyprotech System Simulator (HYSYS) software was used in simulating the process plants and Microsoft Excel was used for exergy, energy and process cost analyses. Annual profit was used as fiscal index for comparism with existing plant design. Exergy analysis of Linde air separation process showed that exergy efficiency of the existing plant (base case) was 3.23 kJ/h while that of the improved plant when the valve was replaced with a turbine (Case 1) was 11.65 kJ/h. Also, the process cost analysis showed that the annual profit for the base case was 48,818,463 ($/yr) while that of the improved case was 50,485,051 ($/yr). Replacing the valve with the turbine in the Linde air separation process could greatly give a better air separation process in terms of high purified medical air with greater annual venture profit.
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Hassan, Alamir H., Zhirong Liao, Kaichen Wang, Mostafa M. Abdelsamie, Chao Xu, and Yanhui Wang. "Exergy and Exergoeconomic Analysis for the Proton Exchange Membrane Water Electrolysis under Various Operating Conditions and Design Parameters." Energies 15, no. 21 (November 4, 2022): 8247. http://dx.doi.org/10.3390/en15218247.

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Integrating the exergy and economic analyses of water electrolyzers is the pivotal way to comprehend the interplay of system costs and improve system performance. For this, a 3D numerical model based on COMSOL Multiphysics Software (version 5.6, COMSOL, Stockholm, Sweden) is integrated with the exergy and exergoeconomic analysis to evaluate the exergoeconomic performance of the proton exchange membrane water electrolysis (PEMWE) under different operating conditions (operating temperature, cathode pressure, current density) and design parameter (membrane thickness). Further, the gas crossover phenomenon is investigated to estimate the impact of gas leakage on analysis reliability under various conditions and criteria. The results reveal that increasing the operating temperature or decreasing the membrane thickness improves both the efficiency and cost of hydrogen exergy while increasing the gas leakage through the membrane. Likewise, raising the current density and the cathode pressure lowers the hydrogen exergy cost and improves the economic performance. The increase in exergy destroyed and hydrogen exergy cost, as well as the decline in second law efficiency due to the gas crossover, are more noticeable at higher pressures. As the cathode pressure rises from 1 to 30 bar at a current density of 10,000 A/m2, the increase in exergy destroyed and hydrogen exergy cost, as well as the decline in second law efficiency, are increased by 37.6 kJ/mol, 4.49 USD/GJ, and 7.1%, respectively. The cheapest green electricity source, which is achieved using onshore wind energy and hydropower, reduces hydrogen production costs and enhances economic efficiency. The growth in the hydrogen exergy cost is by about 4.23 USD/GJ for a 0.01 USD/kWh increase in electricity price at the current density of 20,000 A/m2. All findings would be expected to be quite useful for researchers engaged in the design, development, and optimization of PEMWE.
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Mitrovic, Dejan, Branislav Stojanovic, Jelena Janevski, Marko Ignjatovic, and Goran Vuckovic. "Exergy and exergoeconomic analysis of a steam boiler." Thermal Science 22, Suppl. 5 (2018): 1601–12. http://dx.doi.org/10.2298/tsci18s5601m.

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Relying on coal as primary fuel in thermal power plants represents an unsustainable concept due to limited coal reserves and a negative environmental impact. Efficient utilization of coal reserves and a request for minimization of irreversibilities are imperative for thermal power plants operation. Numerous studies have shown that a steam boiler is a thermal power plant component with the highest irreversibility. The idea of this paper is to quantify the amounts and sources of irreversibilities within a steam boiler and its components, serving a 348.5MWe thermal power plant. Having this in mind, exergy and exergoeconomic analysis of a steam boiler is presented in this paper. Exergy destruction and exergy efficiency of all boiler components and of the boiler as a whole were calculated. Based on exergy flows and economic parameters (cost of the boiler, annual operation hours of the unit, maintenance factor, interest rate, operating period of the boiler), exergy analysis resulted in the cost of produced steam. The obtained results show that the boiler exergy efficiency is at 47.4%, with the largest exergy destruction occurring in the combustion chamber with a value of 288.07 MW (60.04%), and the smallest in the air heater with a value of 4.57 MW (0.95%). The cost of produced steam is calculated at 49,356.7 $/h by applying exergoeconomic analysis.
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Wu, Jin, Jiangjiang Wang, Jing Wu, and Chaofan Ma. "Exergy and Exergoeconomic Analysis of a Combined Cooling, Heating, and Power System Based on Solar Thermal Biomass Gasification." Energies 12, no. 12 (June 24, 2019): 2418. http://dx.doi.org/10.3390/en12122418.

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The purpose of this paper is to improve the utilization of renewable energy by exergy and exergoeconomic analysis of the novel combined cooling, heating, and power (CCHP) system, which is based on solar thermal biomass gasification. The source of heat to assist biomass and steam gasification is the solar heat collected by a dish collector, and the product gas being fuel that drives the internal combustion engine to generate electricity and then to produce chilled/hot water by a waste heat unitization system. The analysis and calculation of the exergy loss and exergy efficiency of each component reveal the irreversibility in the heating and cooling conditions. Then, the exergoeconomic costs of multi-products such as electricity, chilled water, heating water, and domestic hot water are calculated by using the cost allocation method based on energy level. The influencing factors of the unit exergy cost of products are evaluated by sensitivity analysis, such as initial investment cost, biomass cost, service life, interest rate, and operating time coefficient. The results reveal that the internal combustion engine takes up 49.2% of the total exergy loss, and the most effective method of products cost allocation is the exergoeconomic method based on energy level and conforms to the principle of high energy level with high cost.
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Martínez, Amaya, Javier Uche, Carlos Rubio, and Beatriz Carrasquer. "Exergy cost of water supply and water treatment technologies." Desalination and Water Treatment 24, no. 1-3 (December 2010): 123–31. http://dx.doi.org/10.5004/dwt.2010.1368.

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40

El-Nashar, Ali M. "Exergy and cost accounting of the UANE cogeneration plant." Energy 15, no. 11 (November 1990): 1051–60. http://dx.doi.org/10.1016/0360-5442(90)90031-v.

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41

Awaludin Martin, Nur Indah Rivai, Rahmat Dian Amir, and Nasruddin. "Exergoeconomic Analysis of 21.6 MW Gas Turbine Power Plant in Riau, Indonesia." Journal of Advanced Research in Fluid Mechanics and Thermal Sciences 84, no. 1 (July 1, 2021): 126–34. http://dx.doi.org/10.37934/arfmts.84.1.126134.

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In this study, exergoeconomic analysis was carry out on a 21.6MW gas turbine power plant by using logbooks record Pekanbaru Unit. The exergy analysis was start to determine the exergy destruction of each component of the power plant based on the first and second laws of thermodynamics and in this study, exergy and economic analysis were combined and used to evaluate the accrued cost caused by irreversibility, including the cost of investment in each component. The exergy analysis results showed that the location of the largest destruction was in the combustion chamber with 21,851.18 kW, followed by the compressor and gas turbine with 8,495.48 kW and 3,094.34 kW, respectively. The economic analysis resulted that the total cost loss due to exergy destruction was 2,793.14$/hour, consisting of compressor 1,066.43$/hour, combustion chamber 1,561.46$/hour and gas turbine 165.25$/hour. The thermal and exergetic efficiency of gas turbine power plant were 24.51% and 22.73% respectively.
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42

Cavalcanti, Eduardo J. C., and Monica Carvalho. "Tackling Dissipative Components Based on the SPECO Approach: A Cryogenic Heat Exchanger Used in Natural Gas Liquefaction." Energies 14, no. 20 (October 19, 2021): 6850. http://dx.doi.org/10.3390/en14206850.

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The cryogenic industry has been experiencing continuous progress in recent years, primarily due to the global development of oil and gas activities. Natural gas liquefaction is a cryogenic process, with the refrigeration system being crucial to the overall process. The objective of the study presented herein is to carry out an exergoeconomic assessment for a dual nitrogen expander process used to liquefy natural gas, employing the SPecific Exergy COsting (SPECO) methodology. The air coolers and throttling valve are dissipative components, which present fictitious unit cost rates that are reallocated to the final product (Liquefied Natural Gas). The liquefaction process has an exergy efficiency of 41.89%, and the specific cost of liquefied natural gas is 292.30 US$/GJ. It was verified that this cost increased along with electricity. The highest exergy destruction rates were obtained for Expander 1 and Air cooler 2. The highest average cost per exergy unit of fuel was obtained for the vertical separator, followed by Air coolers 1 and 2. An assessment of the exergoeconomic factor indicated that both expanders could benefit from a decrease in exergy destruction, improving the exergoeconomic performance of the overall system. Regarding the relative cost difference, all compressors presented high values and can be enhanced with low efforts.
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43

Shamoushaki, Moein, and Mehdi Ehyaei. "Exergy, economic and environmental (3E) analysis of a gas turbine power plant and optimization by MOPSO algorithm." Thermal Science 22, no. 6 Part A (2018): 2641–51. http://dx.doi.org/10.2298/tsci161011091s.

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In this paper, exergy, exergoeconomic, and exergoenvironmental analysis of a gas turbine cycle and its optimization has been carried out by MOPSO algorithm. Three objective functions, namely, total cost rate, exergy efficiency of cycle, and CO2 emission rate have been considered. The design variables considered are: compressor pressure ratio, combustion chamber inlet temperature, gas turbine inlet temperature, compressor, and gas turbine isentropic efficiency. The impact of change in gas turbine inlet temperature and compressor pressure ratio on CO2 emission rate as well as impact of changes in gas turbine inlet temperature on exergy efficiency of the cycle has been investigated in different compressor pressure ratios. The results showed that with increase in compressor pressure ratio and gas turbine inlet temperature, CO2 emission rate decreases, that is this reduction is carried out with a steeper slope at lower pressure compressor ratio and gas turbine inlet temperature. The results showed that exergy efficiency of the cycle increases with increase in gas turbine inlet temperature and compressor pressure ratio. The sensitivity analysis of fuel cost changes was performed on objective functions. The results showed that at higher exergy efficiencies total cost rate is greater, and sensitivity of fuel cost optimum solutions is greater than Pareto curve with lower total cost rate. Also, the results showed that sensitivity of changes in fuel cost rate per unit of energy on total cost rate is greater than the rate of CO2 emission.
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Han, Bing-Chuan, Yong-Dong Chen, Gai-Ge Yu, Xiao-Hong Wu, and Tao-Tao Zhou. "Completely Recuperative Supercritical CO2 Recompression Brayton/Absorption Combined Power/Cooling Cycle: Performance Assessment and Optimization." International Journal of Photoenergy 2022 (May 20, 2022): 1–22. http://dx.doi.org/10.1155/2022/3869867.

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Excessive heat losses and water consumption in cooling units are significant constraints restricting the application circumstances and performances for the SCO2 Brayton cycle, and the heat exchange capacity in the precooler (PRC) is typically 1.5 times that of power generation. Therefore, this research offers a high-integrated combined power/cooling system in which two waste heat exchangers (WHEs) and a rectifier (RET) are used instead of the PRC to achieve 100% exhaust heat recovery. Each component’s energy and exergy models are developed, and the operational characteristics, coupling relationships, and exergy destruction distribution are examined. Results indicate that, when compared to the Brayton cycle, the thermal and exergy efficiency is considerably increased, and the concentration difference and WHE1 pitch point difference have significant influences on system performance. Further exergoeconomic and optimization analysis reveals that the superior exergy case is mostly recommended for relevant thermal and exergy efficiency increasing rates of 13.7% and 9.17%, respectively, and the unit cost is 81.33% that of the base case. Turbine 1 (TUR1) and main compressor (MCP) are the first and second highest cost rates, respectively, and RET and generator (GEN) account for roughly 34% exergy destruction rate and 20% exergy destruction cost rate, respectively. In addition, reducing heat transfer differences in relevant equipment can further promote system performance.
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Valero, A., L. Serra, and J. Uche. "Fundamentals of Exergy Cost Accounting and Thermoeconomics. Part I: Theory." Journal of Energy Resources Technology 128, no. 1 (July 8, 2005): 1–8. http://dx.doi.org/10.1115/1.2134732.

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These two papers resume the theoretical background supporting the main ideas of the exergy cost accounting and the thermoeconomic approach followed by Valero and co-workers. Part I introduces the basic requirements, with a simple example accompanying the dissertations, to calculate the exergy and thermoeconomic costs and to perform the thermoeconomic analysis of a complex system. The connections with other thermoeconomic approaches and schools are briefly explained. Part II presents, as an illustration of the applications of thermoeconomic analysis, some of the most interesting applications of costs to the operation diagnosis and optimization of a complex system, showing the results on the mentioned example presented in Part I.
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46

Thaddaeus, Julius. "Exergy and economic assessments of an organic rankine cycle module designed for heat recovery in commercial truck engines." Indian Journal of Science and Technology 13, no. 37 (October 10, 2020): 3871–83. http://dx.doi.org/10.17485/ijst/v13i37.1299.

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Objectives: To evaluate the energy and exergy performances of a designed ORC system and to quantify loses within the system and measure its output.The study also assesses the economic performance of the ORC system to determine the feasibility of the business. Methods: Thermodynamic analysis assessing the energy performance and cost estimation using manufacturers’ prices to generate generic equations for estimating costs of the components of the designed ORC system. Findings: The results of the exergy evaluation of the ORC show a system thermal efficiency of 6.39%, net power output of 3.10kWe, exergy destruction of 9.07kW, and exergy efficiency of 54.6%. The economic estimation has a capital investment cost of £8,381.98, a specific investment cost of £2,754.36/kWe, annual savings of £1,233.34, and a payback period of 6.8years. Novelty: The use of exergetic method of analysis and the assessment of the potential economic benefits of installing the module in commercial trucks which form part of the acceptance-criteria, using prevailing market prices of the ORC system is an obvious novelty in this study. In addition, the generation and use of curve-fitting plots to obtain the generic equations for computing the approximate costs of the individual components of the system is an integral part of the novelty of this work. Keywords: Organic Rankine cycle; exergy and economic assessment; specific investment cost; capital investment cost; payback period; exhaust heat recovery
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Baghernejad, Ali, and Amjad Anvari-Moghaddam. "Exergoeconomic and Environmental Analysis and Multi-Objective Optimization of a New Regenerative Gas Turbine Combined Cycle." Applied Sciences 11, no. 23 (December 6, 2021): 11554. http://dx.doi.org/10.3390/app112311554.

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Combined cycle systems have an important role in power generation. In the present study, three different configurations of combined Brayton and Rankine cycle system are studied from the perspective of energy, exergy, exergoeconomic and environmental perspectives. Results indicate that it depends on the preferences and criteria of each decision maker to select the best configuration among the three proposed configurations as the final configuration. For the purpose of parametric analysis, the effect of changing various parameters such as compressor pressure ratio, gas turbine inlet temperature on the output work, exergy efficiency, exergy-economic and environmental parameters is studied. In addition, an attempt is made to optimize the performance of combined cycle systems considering three objective functions of exergy efficiency, total cost rate and exergy unit cost of produced electricity.
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Babaelahi, Mojtaba, and Hamed Jafari. "Exergy Cost Analysis of New Method for Efficiency Improvement in Small Gas Turbines Using LNG Cold Exergy." International Journal of Thermodynamics 21, no. 4 (December 4, 2018): 231–39. http://dx.doi.org/10.5541/ijot.457501.

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Lourenço, Atilio Barbosa, and Monica Carvalho. "Exergy, exergoeconomic and exergy-based emission cost analyses of a coconut husk-fired power and desalination plant." International Journal of Exergy 32, no. 3 (2020): 267. http://dx.doi.org/10.1504/ijex.2020.10030513.

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Lourenço, Atilio Barbosa, and Monica Carvalho. "Exergy, exergoeconomic and exergy-based emission cost analyses of a coconut husk-fired power and desalination plant." International Journal of Exergy 32, no. 3 (2020): 267. http://dx.doi.org/10.1504/ijex.2020.108594.

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