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temperature values. Also the values of the exergoeconomic factor and the relative cost difference are calculated for the different cases. From Table 5, it can be concluded that the highest exergy destruction cost rate is the one associated with expander exergy destruction, however, the exergy destruction ratio is higher at the evaporator and the condenser, 37~40% and 30~38%, respectively. Figures 11 to 13 show the effects of the dead state temperature on the exergoeconomic analysis of the system. The dead state temperature is assumed to change in a reasonable range of values. Fig. 11 shows the effect of dead state temperature on the values of the exergoeconomic factor for the ORC system components. Changing the dead state temperature from 0 to 30oC cause a general decrease in the value of the exergoeconomic analysis, but in different ratios. The value of the exergoeconomic factor for the condenser decreases from 70.3% to 26.07%. Also for the regenerative heat exchanger, the values for the exergoeconomic factor changes in a relatively big range from 63.2% to 41.2%. For the expander, evaporator and the pump, the reduction in the factor values were very limited compared with the other components. It changed from 52.3% to 51.4% for the expander, 88.9% to 84.3% for the evaporator and finally, for the pump, it changed from 94.8% to 94.2%. Low value of the exergoeconomic factor indicates that there is a potential to increase the cost savings by improving the component performance and reducing the exergy destruction occurs through it, this may come on the expenses of the capital investment cost of the component [16]. From the exergy and thermoeconomic analyses, the increase in the dead state temperature value generally caused an increase in the cost rate of the exergy destruction in different system components, however, the cost rates of the exergy destruction expressed as percentage of the total cost rate of exergy destruction have different trends with the change in the dead state temperature as shown in Fig. 12. The cost rates of the exergy destruction in the condenser increase from 29.94 to 33.23 $/h with the dead state temperature increase from 0 to 30oC. But as a percent of the total exergy destruction cost rate, it deceased from 6.9 to 5.72%. For the expander, it increased from 187.7 to 194.7$/h while its percentage decreased from 43.6 to 33.5%. The cost rate and its share in the total exergy destruction cost rate increased for the evaporator from 173.9 to 261.4$/h and from 40.4 to 45.05%, respectively. The RHE shows an increase of the exergy destruction cost rate from 37.62 to 89.68 $/h and an increase in its representation in the total amount from 8.7 to 15.4%. The exergy destruction cost rate at the pump increased slightly from 1.22 to 1.36$/h, however, the cost percentage decreased from 0.28 to 0.23%. In Fig. 13, it shows a decrease in the total product cost rate with the increase of the dead state temperature. The change in the total product cost has a linear form. The total cost rate associated with the system exergy destruction increase with around 140$/h for the same temperature change. 8. Conclusions An organic Rankine cycle with a geothermal heat source and isobutane as working fluid is studied thermodynamically, based on energy and exergy concepts. Exergoeconomic analysis is performed on the system, and different economic factors are calculated at different operating parameters. The following remarks can be extracted from this study: 12PDF Image | Exergoeconomic Analyses and Optimization of Geothermal ORC
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