with the collaboration of Iranian Society of Mechanical Engineers (ISME)

Document Type : Research Article

Authors

1 PhD of Mechanical Engineering of Biosystems, Faculty of Agricultural Engineering & Technology, University of Tehran, Tehran, Iran

2 Department of Mechanical Engineering of Biosystems, Urmia University, Urmia, Iran

3 Department of Agricultural Machinery, Faculty of Agricultural Engineering & Technology, University of Tehran, Tehran, Iran

Abstract

Introduction
Sour cherry concentration is a significant agro-industry in the world. In 2016, world production was 13.8 million tons and most of which were processed in the form of concentrate or frozen products. Iran has the 6th rank among the producers of sour cherry and experienced a highly rise (45%) in production in 2016. A conventional energy system evaluation is performed using the energy analysis method. The thermodynamic inefficiencies occurring within the system (factors that cause a gap between performance and ideal state) are not identified and evaluated by energy analysis.
Materials and Methods
Pakdis concentrate production line includes a plate heat exchanger (HE) converter to preheat input juice using condensate water energy and crude juice heat outlet, four multipurpose falling evaporators (E1, E2, E3, E4), a distillation tower for raw juice aromatization (DT) and a juice cooling system (JC).
A thermographic camera (G120EXD, NEC Avio, Japan) was used for thermographic recording. Initial examination of the thermography results showed that the external surface temperature of the equipment except for the evaporators (E1, E2, E3, E4), the boilers (B1, B2, B3) and the condensation tank of the evaporation line (CT1) had very little difference with the ambient temperature around them, and therefore, their heat flux was ignored.
Due to limitations, the mass flow rates of the evaporation line (except for inlet juice) were not measurable, and therefore, energy analysis was used to calculate them. Energy analysis involves the simultaneous resolution of mass and energy balances for a system.
Results and Discussion
The heat loss rate from the first evaporator (E1) was calculated to be 21.23 kW from which mass/energy balances and mass flows were extracted. Also, heat loss rate from utilities E2, E3, E4, and CT1 were calculated from mass-energy balances. Streams 32, 49, 52, and 54 are not utilized and exit the system. Hence, they are assigned as heat loss streams within the evaporation line.
The total energy loss rate in the evaporation line was calculated to be 4920.82 kW which contributes 74.8% of total input energy to the line. However, 73.39% of this loss is assigned to the cooling tower (stream 54). Stream 29 from the 4th stage evaporator enters the condenser, mixes with water, and provides cold water goes to the cooling tower. In the tower, water evaporates and dissipates heat to the environment. Stream 32 is the second loss stream with 14.8%. Also, it should be noted that heat loss from the surface of utilities makes 3.06% of energy loss of the evaporation line which implies that insulations are done properly in utilities.
Evaporation performance may be rated simply and primarily by the steam economy. The value was calculated to be 2.63 in the evaporation line, i.e. 2.63 kg water is evaporated per 1 kg steam injected into the system
Exergy rate in several streams of evaporation line. The exergy rate of fuel and products, exergy efficiency, exergy destruction rate, and exergy destruction ratio for each element of the line were reported. Total input exergy to the evaporation line is 4832.03 kW from which 1045.85 kW is destructed due to irreversibility and 3786.19 kW is dissipated.
Major destruction occurs within barometric condenser (BC), pressure reducing valve (PR), a plate heat exchanger (HE), evaporators 1 and 2 (E1 and E2), cooling tower (CT), and then evaporators 3 and 4 (E3 and E4). The remaining destruction in other utilities is negligible.
Conclusion
Using the first and second laws of thermodynamics and instrumentation procedure, sub-systems of the evaporation unit of Pakdis Company were investigated and energy and exergy balances were coupled and solved. Thermographic assessment of likely zones to energy losses was employed. The whole process was monitored and mass-energy balances were developed. The steam economy as a reliable criterion for evaporation was calculated. To extract inefficiencies and possible optimizable unit operations exergetic analyses were carried out and subsequently the share of exergy loss and destruction and capital cost in the whole process was defined. It was found that capital cost is consistently ignorable compared to exergetic faults such as losses and destructions.

Keywords

Open Access

©2020 The author(s). This article is licensed under Creative Commons Attribution 4.0 International License (CC BY 4.0), which permits use, sharing, adaptation, distribution and reproduction in any medium or format, as long as you give appropriate credit to the original author(s) and the source.

  1. Akbari, N. 2018. Introducing and 3E (energy, exergy, economic) analysis of an integrated transcritical CO2 Rankine cycle, Stirling power cycle and LNG regasification process. Applied Thermal Engineering 140: 442-454.
  2. Assari, M. R., T. H. Basirat, E. Najafpour, A. Ahmadi, and I. Jafari. 2014. Exergy modeling and performance evaluation of pulp and paper production process of bagasse, a case study. Thermal Science 18 (4): 1399-1412.
  3. Atmaca, A., and R. Yumrutaş. 2014a. Thermodynamic and exergoeconomic analysis of a cement plant: Part I-Application. Energy Conversion and Management 79: 790-798.
  4. Atmaca, A. and R. Yumrutaş. 2014b. Thermodynamic and exergoeconomic analysis of a cement plant: Part II-Application. Energy Conversion and Management 79: 799-808.
  5. Balkan, F., N. Colak, and A. Hepbasli. 2005. Performance evaluation of a triple‐effect evaporator with forward feed using exergy analysis. International Journal of Energy Research 29 (5): 455-470.
  6. Bapat, S., V. Majali, and G. Ravindranath. 2013. Exergetic evaluation and comparison of quintuple effect evaporation units in Indian sugar industries. International Journal of Energy Research 37 (12): 1415-1427.
  7. Bapat, S., V. Majali, and G. Ravindranath. 2016. Exergy and sustainability analysis of quintuple effect evaporation unit in a sugar industry-a case study. International Journal of Renewable Energy Technology 7 (1): 46-68.
  8. Carlomagno, G. M., and G. Cardone. 2010. Infrared thermography for convective heat transfer measurements. Experiments in fluids 49 (6): 1187-1218.
  9. Carlomagno, G. M., L. de Luca, G. Cardone, and T. Astarita. 2014. Heat flux sensors for infrared thermography in convective heat transfer. Sensors 14 (11): 21065-21116.
  10. Cengel, Y. 2011. Thermodynamics an Engineering Approach. 5th Edition by Yunus A Cengel, Thermodynamics an Engineering Approach, Digital Designs.
  11. Cengel, Y. 2014. Heat and mass transfer: fundamentals and applications, McGraw-Hill Higher Education.
  12. Costa, M. M., R. Schaeffer, and E. Worrell. 2001. Exergy accounting of energy and materials flows in steel production systems. Energy 26 (4): 363-384.
  13. Dincer, I., and M. A. Rosen. 2005. Thermodynamic aspects of renewables and sustainable development. Renewable and Sustainable Energy Reviews 9 (2): 169-189.
  14. Dincer, I. 2018. Comprehensive energy systems, Elsevier.
  15. FAO. 2018. https://www.fao.org/news/archive/news-by-date/2018/en/ (accessed April 25, 2020).
  16. Forero-Núñez, C. A., and F. E. Sierra-Vargas. 2016. Heat Losses Analysis Using Infrared Thermography on a Fixed Bed Downdraft Gasifier. International Review of Mechanical Engineering 10 (4): 239-246.
  17. Hosseini, S. S., M. Aghbashlo, M. Tabatabaei, H. Younesi, and G. Najafpour. 2015. Exergy analysis of biohydrogen production from various carbon sources via anaerobic photosynthetic bacteria (Rhodospirillum rubrum). Energy 93: 730-739.
  18. Kamate, S., and P. Gangavati. 2009. Exergy analysis of cogeneration power plants in sugar industries. Applied Thermal Engineering 29 (5-6): 1187-1194.
  19. Lazaretto, A., and G. Tastasaronis. 2006. SPECO: A systematic and general methodology for calculating efficiencies and costs in thermal systems 31 (1): 1257-1289.
  20. Lorenz, F. 2008. Improving energy efficiency in sugar processing Handbook of Water and Energy Management in Food Processing. Elsevier.
  21. Piri, A., A. M. Nikbakht, and H. Janisarnavi. 2019. Journal of Researches in Mechanics of Agricultural Machinery 8: 66-57
  22. Ramedani, Z., R. Abdi, M. Omid, and A. Maysami. 2018. Evaluating the Energy Consumption and Environmental Impacts in Milk Production Chain (Case Study: Kermanshah City of Iran). Journal of Agricultural Machinery 8 (2): 435-447. (In Persian). http://dx.doi.org/10.22067/jam.v8i2.63570.
  23. Simionescu, Ş. M., Ü. Düzel, C. Esposito, Z. Ilich, and C. Bălan. 2015. Heat transfer coefficient measurements using infrared thermography technique. Paper presented at the Advanced Topics in Electrical Engineering (ATEE), 9th International Symposium.
  24. Sogut, Z., N. Ilten, and Z. Oktay. 2010. Energetic and exergetic performance evaluation of the quadruple-effect evaporator unit in tomato paste production. Energy 35 (9): 3821-3826.
  25. Soufiyan, M., M. Aghbashlo, and H. Mobli. 2016. Journal of Cleaner Production 1-18.
  26. Tsatsaronis, G. 1993. Thermoeconomic analysis and optimization of energy systems. Progress in Energy and Combustion Science 19 (3): 227-257.
  27. Xiang, J., M. Cali, and M. Santarelli. 2004. Calculation for physical and chemical exergy of flows in systems elaborating mixed‐phase flows and a case study in an IRSOFC plant. International Journal of Energy Research 28 (2): 101-115.
  28. Yildirim, N., and S. Genc. 2017. Energy and exergy analysis of a milk powder production system. Energy Conversion and Management 149: 698-705.
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