Poredos, A.

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Purdue UniversityPurdue e-PubsInternational Refrigeration and Air ConditioningConference School of Mechanical Engineering1996Exergy Analysis of Vapour and Sorption CoolingProcessesA. PoredosUniversity of LjubljanaFollow this and additional works at: http://docs.lib.purdue.edu/iraccThis document has been made available through Purdue e-Pubs, a service of the Purdue University Libraries. Please contact epubs@purdue.edu foradditional information.Complete proceedings may be acquired in print and on CD-ROM directly from the Ray W. Herrick Laboratories at https://engineering.purdue.edu/Herrick/Events/orderlit.htmlPoredos, A., "Exergy Analysis of Vapour and Sorption Cooling Processes" (1996). International Refrigeration and Air ConditioningConference. Paper 333.http://docs.lib.purdue.edu/iracc/333EXERGY ANALYSIS OF VAPOUR AND SORPTION COOLING PROCESSES Alojz Poredos Faculty of Mechanical Engineering, Ljubljana, Slovenia ABSTRACT Exergy is precious energy. On the basis of thermodynamic analysis of thermal processes, one can choose more exergy-saving devices. This is especially important in refrigeration processes, in which the consumption of energy and exergy increases considerably with the falling cooling temperature. The exergy efficiency in terms of exergy losses of vapour compression and sorption cooling processes is analysed in the paper. In the case of vapour compression processes, analysis of the influence parameters on exergy efficiency shows a strong dependence on the cooling temperature. Exergy efficiency of sorption processes depends mainly on cooling and regeneration temperature. A comparison of exergy efficiencies of vapour compression and sorption cycles has been made for average values of working parameters. B - anergy (J) E - exergy (J) Q - heat quantity (J) T - temperature (K) Indexes a -actual am -ambient ave - actual, vapor compression as - actual, sorption Ca -Camet's exvc - exergetic, vapor compression exs - exergetic, sorption h -heating NOMENCLATURE t - temperature CC) W- energy (J) '11 - efficiency (-) ha hr lvc Is R s vc - heating, actual - heating, reversible - losses, vapor compression - losses, sorption - refrigeration -sorption - vapor compressiOn 1. INTRODUCTION The basic task of a cooling device is heat output from the cooled system, which is at a lower temperature than its surroundings. The majority of cooling devices utilize the vapour cooling process and a mechanical compressor driven by electric energy. The proportion of refrigerators based on different sorption processes, driven by a heat compressor, has increased lately. In both types of refrigeration· device heat is transferred from the cooled system at temperature T R into the surroundings. A vapour compressor device is driven by a mechanical compressor utilizing technical work W (electric power), which is pure exergy, to increase the temperature and pressure level of the heat QR. A sorption refrigerator operates with a heat compressor driven by heat Qg without converting it into electrical or mechanical energy. 253 Sorption refrigeration devices are one ofthe alternatives for ecologically acceptable cooling. Any form of heat at an appropriate temperature level can be used to drive such coolers. One advantage of sorption cooling devices over vapour compressor cooling devices is the possibility of utilizing waste heat with little exergy and the direct use of alternative energy sources. 2. EXERGY OF COOLING ENERGY A precisely determined mixture of exergy and anergy is required for the functioning of a cooling device based on vapour and sorption processes [ 1 ], [2]. In general, the cooling energy consists of exergy and anergy: QR =ER +BR (1) whereby the share of exergy is: ( Tam) ER =~1--·IQR \ TR) (2) and the share of anergy is Tam BR = TR QR· (3) At a higher ambient temperature and a lower temperature of the cooled system, more exergy ER is needed for heat output QR from the cooled system. 3. EXERGY LOSS IN VAPOUR COOLING PROCESSES A vapour cooling device operates in the temperature range between the temperature of the cooled system TR and the ambient temperature Tam. Its task is the input of the necessary share of exergy ER into the cooled system for the output of anergy BR from the cooled system. Figure 1 shows the Rant diagram for reversible and irreversible cooling cycles. BR BR Cooled system TR Cooled system TR Fig. 1. Energy flows in a) a reversible and b) an irreversible vapour compressor cooling process 254 In both cases, the cooling energy equals QR and eq. (I) is applied. In the case of a reversible cooling process, the necessary driving energy is: Wr=ER. (4) However, in an irreversible, i.e. a real process, exergy loss must be added: Wa = Wr +E1vc (5) If cooling processes were reversible, heat output into the surroundings would be: Qrvc = BR + Wr (6) and in real processes: (7) A thermodynamic assessment of real cooling processes can be obtained through the exergy efficiency, which represents the degree of reversibility ofthe process: = [ER/ = jERj < 1 (S) ~e~c - · Wa Wr +EJvc Its relationship to the cooling coefficient of performance (COP): COP = QR (9) Vc W a IS: COPvc ~e~c =COP Ca T -TR am COP TR vc (10) The COP of a vapour cooling process depends on numerous influential parameters and above all on the temperature conditions and the working fluid. Analysis of the exergy efficiency and exergy loss of a vapour cooling process depending on the cooling temperature for the refrigerants R22, Rl34a and NH3 at a constant condensation temperature of 40°C and compressor efficiency of 0. 7 was therefore made. The r~sults ofthe analysis are shown in figures 2 and 3_ 0.4 ~ ~ '2j ~ ' 0.3 --o---- NH3 0.1 - -o-R22 ~Rl34a I I I ' 0 -30 0 10 Fig. 2. Exergy efficiency of a vapour compressor cooling process vs. evaporation temperature 0.5 -----<>--- NH3 ~ ---o- R22 ~ --6---- Rl34a ------. ~ ~-----. --0.4 6 0.3 --~ 0.2 ~ 0.1 0 - -30 -20 0 10 Fig. 3. Specific exergy loss of vapour cooling processes vs. cooling temperature 255 The exergy efficiency falls with increases in the cooling temperature. Similar findings are given in [3]. The ammonia vapour cooling process is most efficient in the low temperature range. Increases of the cooling temperature reduces these differences. Results for R22 and R134a are fairly similar. The equation for specific exergy loss is obtained by combining eqs. (4) and (5) and by taking into account the exergy of the cooling energy : E1vc 1 Tam ~ TR --~ =---QR ~ COPvc TR COPvc 1 1 (11) CO Pea The exergy loss in figure 3 decreases with increases in the cooling temperature. This is caused by the large temperature dependence of the Camot coeficient COP ca in the same way as for the real process coeficient COP rc-4. EXERGY LOSS IN SORPTION COOLING PROCESSES Heat used to drive sorption cooling devices usually has little exergy. It was established for vapour cooling processes that a precisely determined amount of exergy ER is needed for cooling energy QR output from a cooled system. The same applies to sorption cooling processes. According to the Rant diagram shown in figure 4a for a reversible sorption cooling process, in which energy flows were presented, the necessary energy input is: (12) This energy has to be at a temperature higher than that of the surroundings. In the case of a real sorption cooling process as in figure 4b, exergy loss occurs, so the amount of energy for heating is increased by Ets and by the appertaining share of energy. Thus: (13) Ambience Qrs Ambience Cooled system T R Cooled system T R Fig. 4. Energy flows in a) a reversible and b) an irreversible sorption cooling process The total energy output from a real process and a cooled system into its surroundings is the sum of the anergy ofheat, exergy loss in the process and the anergy of the cooling energy: 256 (14) The exergy efficiency of a sorption cooling process is defined analogously as in the vapour cooling process: the mechanical work input is replaced by heat: jERj jERj llexs = --= ::;; 1 Eha Ehr +E1s (15) Taking into account the expression for the COP of a sorption cooling process: COPs= QR Qha (16) and eq. (2), the relationship between the exergy efficiency of a sorption cooling process and the COP on the one hand, and temperature conditions on the other, can be obtained: 0.5 -¢-- T g=80°C -o- T g=90°C 0.1 ---&--- Tg=l00°C -x- Tg=ll0° t+------"'~ -x- Tg=l20°C --o- Tg=l30° ------ T g= l40°C -+--- T g= 150° 0 -30 -20 -10 0 10 tR(OQ Fig 5. Exergy efficiency of the sorption cooling process with the working pair NH3-HzO vs. cooling and heating temperature 0.6 0.5 0.1 0 -30 (17) -<>--- Tg=80°C -t.- Tg=l00°C -x- Tg=l20°C -Tg=l40°C -20 -10 tRee> -o-- Tg=90°C -x- Tg=I 10°C --o- Tg=I30°C -+---- T g= l50°C 0 X ---x 10 Fig. 6. Specific exergy loss in an ammonia-water sorption cooling process in dependence on the cooling and the heating temperature The dependence of the exergy efficiency of the sorption cooling process with the ammonia - water working pair on the cooling and the heating temperature is shown in Fig. 5. As is the case for compressor cooling devices, efficiency decreases with an increase in the cooling temperature. Its value also decreases with an increase in the heating temperature. 257 Similar results were reported by Ercan ( 4), who has performed an analysis of individual components of a sorption system. The following expression is obtained from eq. (14) for specific exergy loss in a sorption cooling process by taking into account the exergy of the cooling energy and the heating energy: Els - 1 QR COPs (18) Figure 6 shows that a similar dependence exists in the exergy sorption process loss to that in the exergy efficiency. The lower the heating temperature and the higher the cooling temperature, the lower the exergy loss would be. 5. CONCLUSIONS The exergy loss has a double negative effect. Firstly, it increases the work required to drive the cooling device and, secondly, higher heat output is needed for the condenser, so that a larger heat transfer surface is required. An overall thermodynamic analysis of vapour and sorption cooling processes has been performed. R22, R134a and ammonia refrigerants have been compared in the simple vapour cooling devices. No significant differences were pointed out. Slightly more favourable results were found for ammonia usage. The simple sorption cooling process was analysed for the ammonia - water pair. Similar dependence of the exergy efficiency and loss were performed in both cooling processes. The exergy comparison of vapour compression and sorption cooling processes shows that cooling based on sorption is more convenient than vapour cooling cycles when they are driven by a lower heating temperature. Using higher heating temperature (in our case more than 1 00°C) the vapor cooling · process becomes more exergy convenient. In addition to the exergy analysis, the following has to be taken into consideration in choosing a cooling device operating on the basis of a vapour or sorption process. Vapor compresion cooling devices are more efficient in terms of energy (a higher COP). They consume pure exergy. They are more compact. Sorption cooling devices use energy with little exergy, mainly in the form of waste heat, the exergy value of which is close to 0 in the case of non-utilization. They are environmentally friendly. They have to assure the flow of a large amount of anergy, which is also contained in waste heat This in tum means that a large surface is required for heat transfer. The weight per unit of cooling power is thus considerably greater than in the case of vapour cooling devices, which increases investment costs. 6. REFERENCES [1] RantZ. : Termodymamics. University, Ljubljana 1963. [2] Baehr H. D. : Thermodynamik, Springer Verlag, Berlin 1989. [3] Opresnik M. : Exergy losses of cooling and heating processes, J. Mech. Eng., 1969 (1) 2-5. [4] Ercan 0., Gogiis Y.: Comparative study ofirreversibities in an aqua- ammonia absorption refrigeration system, Int. J. Refrig. 1991, (14), 86-92. , [5] Arh S. :Master Thesis, Faculty ofMechanical Engineering, Ljubljana 1988. 258 

Exergy Analysis of Vapour and Sorption Cooling Processes

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Exergy Analysis of Vapour and Sorption Cooling Processes

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