Open access peer-reviewed chapter

Exergy Flows Inside Expansion and Compression Devices Operating below and across Ambient Temperature

By Mikhail Sorin and Mohammed Khennich

Submitted: October 12th 2017Reviewed: January 15th 2018Published: February 20th 2018

DOI: 10.5772/intechopen.74041

Downloaded: 124

Abstract

The various definitions of the coefficient of exergy efficiency (CEE), which have been proposed in the past for the thermodynamic evaluation of compression and expansion devices, operating below and across ambient temperature as well as under vacuum conditions, are examined. The shortcomings of those coefficients are illustrated. An expression for the CEE based on the concept of transiting exergy is presented. This concept permits the quantitative and non-ambiguous definition of two thermodynamic metrics: exergy produced and exergy consumed. The development of these CEEs in the cases of an expansion valve, a cryo-expander, a vortex tube, an adiabatic compressor and a monophasic ejector operating below or across ambient temperature is presented. Computation methods for the transiting exergy are outlined. The analysis based on the above metrics, combined with the traditional analysis of exergy losses, allows pinpointing the most important factors affecting the thermodynamic performance of sub-ambient compression and expansion.

Keywords

  • exergy efficiency
  • expansion
  • compression
  • sub-ambient
  • across ambient

1. Introduction

Cooling is part of twenty-first century life. Air conditioning, food conservation, industries such as steel, chemicals, and plastics depend on cooling. By mid-century people will use more energy for cooling than heating [1]. Almost all cold is produced by vapor-compression refrigeration and requires large amounts of electricity for its production. And since electricity is still overwhelmingly produced by burning fossil fuels, the rise in cold production will inevitably increase both fuels consumption and power plant emissions. A climate-change irony is that cooling makes the planet hotter. Besides the development of new cooling devices using renewable energy, an important way to reduce refrigeration power consumption is through the energy efficiency improvement of vapor-compression cycles and their associated elementary processes. The processes of compression and expansion play a central role in air-conditioning, refrigeration and cryogenics. An important question still remains: How to define the efficiency of these processes by taking into account the constraints of the first and second laws of thermodynamics? The answer will be discussed in this paper.

The introduction of exergy, the thermodynamic function that takes into account the quality as well as the quantity of energy, has paved the way for a unified approach to the concept of efficiency, a subject pioneered by Grassmann [2]. Serious difficulties concerning the practical application of this concept to sub-ambient systems, however, retarded the acceptance of exergy analysis by the air-conditioning and refrigeration engineering profession. One can mention, in particular, the difficulty of formulating a coefficient of exergy efficiency (CEE) for elementary processes such as compression and expansion. The coefficient should evaluate the exergy losses, quantify the extent to which the technical purpose of an elementary process is achieved, as well as quantify the exergy consumption within the process. Finally, a uniquely determined value (not several) should be assigned to the coefficient. This paper examines some important points pertinent to these issues and presents a definition of the CEE for the thermodynamic evaluation of expansion and compression devices operating below and across ambient conditions. The definition is based on the concept of transiting exergy, introduced by Brodyansky et al. [3], that allows non-ambiguous computation of two metrics: exergy produced and exergy consumed.

2. Basic concepts of exergy analysis of sub-ambient systems

The maximum amount of work obtained from a given form of energy or a material stream, using the environment as the reference state, is called exergy [4, 5]. Three different types of exergy are important for thermodynamic analysis of the sub-ambient processes: exergy of heat flow, exergy of work (equivalent to work) and thermo-mechanical exergy, also known as physical exergy by some authors [4, 6]. Chemical exergy [7], important for some refrigeration systems based on the mixing of streams of different composition, is not considered in the present paper.

2.1. Exergy of heat flow at the sub-ambient conditions

The exergy of heat flow Q̇[4] is defined as:

ĖQ=Q̇ΘE1

where Θ = 1 − T0/T is the Carnot factor determined by the temperature T of heat flow, and the ambient temperature T0. Contrary to conditions above ambient, Θ is negative for sub-ambient temperatures. However, according to Eq. (1), ĖQis positive due to the fact that heat is removed from a cooled object, and thus Q̇has a negative sign in Eq. (1). The energy and exergy balances of a reversible refrigerator (RR) are presented in Figure 1. One can notice that the directions of energy and exergy flows are opposite below T0. This means that the exergy of a heat flow at T < T0 is looked upon as a product of the refrigeration system rather than as feed. The exergy transfer of a RR characterizes the rate of transformation of power Ẇto exergy of heat flow Q̇(exergy of produced cold). Given that the system presented in Figure 1 is reversible, the minimum power Ẇminnecessary to maintain a cooling rate Q̇equals ĖQ. Obviously it is not the case for a real (non-reversible) refrigerator, where ĖQis lower than Ẇby the value of exergy losses Ḋ.

Figure 1.

Energy (a) and exergy (b) balances of a reversible refrigerator (RR).

2.2. Thermo-mechanical exergy

The thermo-mechanical exergy equals the maximum amount of work obtainable when the stream of substance is brought from its initial state to the environmental state, defined by pressure P0 and temperature T0, by physical processes involving only thermal interaction with the environment [3, 4]. The specific thermo-mechanical exergy eP,T is calculated according to:

eP,T=hPTh(P0T0)T0sPTs(P0T0)E2

The value of eP,T may be divided by two components: thermal exergy eT due to the temperature difference between T and T0, and mechanical exergy eP due to the pressure difference between P and P0. It is important to emphasize that this division is not unique, because eT depends on pressure conditions and eP in its turn depends on temperature conditions. As a result, the division has no fundamental meaning and leads, as will be illustrated further, to ambiguities for the exergy efficiency definition. By conventional agreement [4], eT and eP are defined as:

eT=hPTh(PT0)T0sPTs(PT0)E3
eP=hPT0h(P0T0)T0sPT0s(P0T0)E4

The contribution of eT and eP to the value of eP,T can be clearly visualized on the exergy-enthalpy diagram presented in Figure 2. For instance, the thermal exergy for point 1 is illustrated as the segment (eT)1 defined by the intersections of two isotherms T1 and T0 with the isobar P1. The mechanical exergy for point 1 is illustrated as the segment (eP)1 defined by the intersections of two isobars P1 and P0 with the isotherm T0. Whatever the temperature conditions are (T < T0 or T > T0), the thermal exergy is always positive [3], as clearly presented on the e-h diagram. In this sense the eT behavior is similar to that of the exergy of heat flow, that is always positive, as has been discussed. Meanwhile, eP is only positive for conditions P > P0 (see for example point 1), but it is negative for P < P0, as illustrated by point 2 in Figure 2.

Figure 2.

Thermal eT and mechanical eP exergy components on an exergy-enthalpy diagram.

2.3. Exergy efficiency of processes operating below and across the ambient temperature

The exergy balance around any process under steady state conditions and without external irreversibilities (the case considered in this paper) may be written as [4]:

Ėin=Ėout+ḊintE5

Here Ėinand Ėoutare the inlet and outlet exergy flows; Ḋintis the rate of internal exergy losses. There is abundant scientific literature [3, 4, 5, 6, 7, 8, 9] on the subject of the exergy performance criteria definition based on Eq. (5). However, there are only a few definitions of this criteria applied to the processes of expansion and compression operating below and across ambient temperature. Among them, three exergy efficiency definitions may be distinguished: input-output efficiency, products-fuel efficiency, and efficiency that accounts for the transiting exergy.

The input-output efficiency ηin-out, first proposed by Grassmann [2], is computed according to Eq. (6):

ηinout=ĖoutĖinE6

The shortcomings of this definition, particularly for its application to sub-ambient problems, are well documented [3, 4, 5, 6, 7, 8, 9]. The main one is the fact that often ηin-out does not evaluate the degree to which the technical purpose of a process is realized; the subject will be illustrated in Section 3. The products-fuel efficiency ηpr-f proposed by Tsatsaronis [10] and Bejan et al. [6] in the context of expansion and compression processes is computed as:

ηprf=Exergy of ProductsExergy of FuelE7

Under the terms “products” and “fuel” the authors meant either the differences in exergies of the streams at the inlet and outlet of a process, or the exergies of streams themselves. For example, while evaluating the efficiency of an adiabatic compression operating above ambient conditions, the “fuel” is the supplied work, and the “product” is the increment of thermo-mechanical exergy. The problem with this approach is that it is possible to obtain different values of ηpr-f of the sub-ambient expansion and compression processes due to the fact that different things can be understood under the notions “products” and “fuel”. It should be also mentioned that some authors used a different terminology to express the numerator and denominator of Eq. (7). For example, Kotas [4] used “desired output” vs. “necessary input”; Szargut et al. [5] used “exergy of useful products” vs. “feeding exergy”.

Brodyansky et al. [3] proposed a definition of efficiency based on the subtraction of the exergy that has not undergone transformation within an analyzed process. The latter was named “transiting exergy”, Ėtr, and the exergy efficiency is defined as:

ηtr=ĖoutĖtrĖinĖtr=ΔĖĖE8

where ΔĖand ∇Ėare the exergy produced and exergy consumed in the process. It is clear that the difference between the denominator and the numerator in Eq. (8) equals the exergy losses within the process. It will be illustrated that the unambiguous definition of Ėtrpaves the way for the uniquely determined thermodynamic metrics ΔĖand ∇Ėin the case of thermo-mechanical exergy transformation for sub-ambient processes. The evaluation of ηtr to assess the rate of exergy transfer of the mechanical exergy component to the thermal exergy component for these processes will be based on these metrics.

3. Transiting thermo-mechanical exergy and its link to the thermal and mechanical components

Following the equations proposed by Brodyansky et al. [3], the specific transiting thermo-mechanical exergy etr of an analyzed system is defined as the minimum exergy value that can be assigned to a material stream, considering the pressure P and temperature T at the inlet and outlet, as well as the ambient temperature T0. With this definition, there are three possible combinations of Pin, Tin, Pout, Tout and T0 that determine the value of etr:

IfTin>T0andTout>T0:Ėtr=ṁ.etrPminTminE9a
IfTin<T0andTout<T0:Ėtr=ṁetrPminTmaxE9b
IfTin>T0andTout<T0ORTin<T0andTout>T0:Ėtr=ṁetrPminT0E9c

Inspection of these equations shows that for all three cases etr is determined by using the lowest pressure Pminamong the inlet and outlet values. The situation is different for temperature, where the minimum exergy value is determined using the lowest temperature Tminfor processes above ambient, the highest temperature Tmaxfor sub-ambient processes, and by using T0 for the case of processes operating across ambient temperature. In order to understand the physical meaning of the transiting exergy, let us analyze the throttling process of a real gas taking place under these three different temperature conditions.

3.1. Adiabatic throttling process

The case of the throttling process operating above T0 is presented on an e-h diagram (see Figure 3a). According to Eq. (9a), the value of etr is:

etr=ePoutToutE10

Figure 3.

Transiting thermo-mechanical exergy presentation for a throttling process of a real gas operating above (a), below (b), and across (c) ambient temperature (T0).

This value coincides with the value e2 as illustrated in Figure 3a. The specific exergy losses (d) are also presented on the diagram. Following Eq. (8), the values ΔĖand ∇Ėare:

ΔĖ=ṁeoutetr=0E11
Ė=ṁeinetr=ṁdE12

where ṁis the gas mass flow rate.

As a result, the efficiency ηtr = 0, meaning that the exergy consumed is completely lost during the process and there is no produced exergy. It should be mentioned that the input-output efficiency calculated according to Eq. (6) has a negative value in this particular case and has no physical meaning. This is due to the fact that Ėout< 0, because the throttling ended at the vacuum conditions. For this particular case the products-fuel efficiency according to Eq. (7) gives the same value as ηtr.

Now, let us analyze the case of throttling at sub-ambient conditions presented in Figure 3b. According to Eq. (9b):

etr=ePoutTinE13

Thus ΔĖand ∇Ėare calculated as:

ΔĖ=ṁeoutetr=ṁePoutToute(PoutTin)=ṁΔeTPoutE14
Ė=ṁeinetr=ṁePinTine(PoutTin)=ṁePTinE15

The term (ΔeT)Pout in Eq. (14) is the increase of the specific thermal exergy due to an isobaric temperature drop under sub-ambient conditions at constant pressure Pout. The term (∇eP)Tin in Eq. (15) is the decrease of the specific mechanical exergy due to an isothermal pressure drop at constant temperature Tin. Finally, the case presented in Figure 3c illustrates a throttling process started above ambient and ended at sub-ambient conditions. According to Eq. (9c):

etr=ePoutT0E16

The values ΔĖand ∇Ėare calculated as:

ΔĖ=ṁeoutetr=ṁePoutToute(PoutT0)=ṁΔeTPoutE17
Ė=ṁeinetr=ṁePinTine(PoutT0)=ṁeP,TE18

Again, the input-output efficiency is not suitable for the evaluation of the processes presented in Figure 3b and c, given that the outlet exergy e2 = e(Pout, Tout) is negative. Another difficulty is linked to the application of the products-fuel efficiency for these cases. The exergy transfer of the throttling process at sub-ambient conditions consists in the partial transformation of mechanical exergy (“fuel”) into thermal exergy (“product”). The problem stems from the fact that there are multiple possibilities to define “fuel” and “product” in this case; as a result multiple values of ηpr-f may be formulated, leading to the ambiguity in the products-fuel efficiency application. Indeed, the different increments of thermal exergy may be considered as a “product” for the case in Figure 3b, for example, the increase in thermal exergy following the isobar P1 or the isobar P2. In the same way, different decrements of mechanical exergy may be considered as a “fuel” in the same figure, for example, the decrease of mechanical exergy following the isotherms T1 or T2.

Contrary to “products-fuel”, the transiting exergy approach does not attempt to individually compute the thermal and mechanical exergy component variations. It relies, rather, on the unaffected part of the thermo-mechanical exergy entering and leaving the system.

As illustrated in Figure 3a and c, the transiting exergy may be considered as the introduction of a new reference state to evaluate exergy consumed and produced. Instead of the reference point e = 0 (the intersection of the isobar P0 and the isotherm T0), the new reference point is presented by etr: the intersection of the isobar P2 and the isotherm T2 for the case 3a; of the isobar P2 and the isotherm T1 for the case 3b; and of the isobar P2 and the isotherm T0 for the case 3c. Finally, the transiting exergy approach provides the foundation for the non-ambiguous definition of the terms ΔĖand ∇Ė, and thus of ηtr.

Example 1

The initial parameters of air at the inlet of a throttling valve are: ṁ= 1 kg/s, P1 = 3 MPa, T1 = 140 K. The ambient temperature T0 = 283 K. Calculate the variation of Ėtr, ΔĖand ∇Ėand ηtr as a function of the outlet pressure P2 in the range 0.1–1 MPa.

Solution

The outlet temperature of the air is calculated by using the software Engineering Equation Solver (EES) [11]. Given that the expansion of air takes place at sub-ambient conditions, Eqs. (13)(15) are used to evaluate Ėtr, ΔĖand ∇Ė. The results are presented in Table 1. One observation is obvious, that the rise in exergy losses as well as the decrease in ηtr go along with the decreasing outlet pressure P2. Less obvious is that the exergy produced ΔĖrises with decreasing P2, reflecting the production of a more important cooling effect. It can also be noticed that the transiting exergy Ėtrdecreases with decreasing outlet pressure P2.

Example 2

The expansion valve of a refrigeration mechanical vapor compression cycle is supplied with the subcooled working fluid R152a at the rate ṁ= 0.15 kg/s at P1 = 615.1 kPa. The fluid is expanded to a pressure of P2 = 142.9 kPa. The ambient temperature T0 = 278 K. Calculate the variation of Ėtr, ΔĖand ∇Ėand ηtr as a function of the subcooling ΔTsubC in the range 275–281 K.

Solution

A vapor compression cycle is presented on a Ts-diagram in Figure 4. The subcooling process is represented by the line 3f-3. Given that the expansion of R152a takes place across ambient temperature, Eqs. (16)(18) are used to evaluate Ėtr, ΔĖand ∇Ė. The results are shown in Table 2.

The transiting exergy does not change with the subcooling, because it is the function of constant parameters T0 and P2, meanwhile the exergy produced increases and exergy consumed decreases. The new result is that ηtr is rising with the subcooling. It should be mentioned that increasing the amount of subcooling is well documented as a way to increase the COP (coefficient of performance) of vapor compression cycles [4]. Thus, the rise in ηtr of an expansion device guarantees the COP improvement of the overall cycle, a conclusion that may lead to practical recommendations for optimization of refrigeration cycles.

P2
(MPa)
T2
(K)
Ė
(kW)
ΔĖ
(kW)
Ḋ
(kW)
Ėtr
(kW)
ηtr
(%)
1.0118.6101.830.871.0245.930.3
0.9117.3110.832.478.4236.929.2
0.7114.7132.035.696.4215.726.9
0.5111.9160.138.8121.3187.624.2
0.3109.1202.342.1160.2145.420.8
0.1106.0292.345.5246.855.515.6

Table 1.

Variation in temperature and exergy metrics with the outlet pressure for a throttling process of air.

Figure 4.

A vapor compression cycle presentation on a Ts-diagram.

ΔTsubC
(K)
Ė
(kW)
ΔĖ
(kW)
Ḋ
(kW)
Ėtr
(kW)
ηtr
(%)
2754.0833.2080.8751.74478.6
2764.0663.2300.8361.74479.4
2784.0343.2740.7601.74481.2
2794.0203.2950.7251.74482.0
2813.9943.3390.6551.74483.6

Table 2.

Variation in exergy metrics with subcooling for the expansion process of R152a.

3.2. Expansion in low temperature systems with work production and heat transfer

The primary purpose of expansion processes in the sub-ambient region is the production of cooling effect. The power that may be produced can be considered as a useful by-product. This type of expansion takes place in cryo-expanders. There are two types of these devices: adiabatic and non-adiabatic gas expansion machines. The energy and exergy balances around a non-adiabatic expander are presented in Figure 5. It should be emphasized that the directions of heat flow Q̇and exergy ĖQare opposite. This is due to the fact that heat transfer from a cooled object to the expanding fluid occurs at T < T0. As a result ĖQcalculated according to Eq. (1) is presented as the outlet flow in Figure 5b.

Figure 5.

Energy (a) and exergy (b) balances around a non-adiabatic cryo-expander.

The process of gas expansion in a non-adiabatic cryo-expander is presented on an e-h diagram (see Figure 6). Similar to the case of adiabatic throttling (Figure 3b), the transiting exergy in the gas flow is defined according to Eq. (9b). As a result, the exergy efficiency is calculated as:

ηtr=ṁΔeTPout+Q̇Θ+ẆTṁePTinE19

Figure 6.

Gas expansion in a non-adiabatic cryo-expander on an exergy-enthalpy diagram.

In the case of an adiabatic cryo-expander ηtr is calculated according to Eq. (19), but with the term Q̇.Θin equals to zero.

Example 3

An adiabatic turbine (ηT = 0.80) is supplied with air at the rate ṁ= 1 kg/s at P1 = 6 MPa, T1 = 320 K. The ambient temperature T0 = 283 K. Calculate the variation of Ėtr, ΔĖand ∇Ėand ηtr as a function of the outlet pressure P2 in the range 0.1–3 MPa.

Solution

Given that the expansion of air takes place across ambient temperature, Eqs. (16)(18) are used to evaluate Ėtr, ΔĖand ∇Ė. ηtr is calculated according to Eq. (19), but with the term Q̇.Θin equals to zero. The results are shown in Table 3. It is illustrated that Ėtrdecreases with P2 reduction, and as a result ΔĖand ∇Ėand Ẇrise, but the increase in ΔĖand Ẇis offset by the greater increase in ∇Ėcausing ηtr to decrease. The negative value of Ėtrin the second last row to the right in Table 3, is because the stream at state 2 is under vacuum conditions. It should be emphasized that the increase in the ΔĖmetric reflects the deeper refrigeration of air with increasing pressure drop in the turbine.

P2
(MPa)
T2
(K)
Ė
(kW)
ΔĖ
(kW)
ẆT
(kW)
Ḋ
(kW)
Ėtr
(kW)
ηtr
(kW)
3.00271.857.90.245.612.1274.279.1
2.55263.868.30.753.014.6263.978.7
2.50255.180.11.561.217.4252.078.2
1.85245.494.12.970.321.0238.077.7
1.50234.3111.14.980.725.5221.177.1
1.15221.2132.68.293.131.3199.676.4
0.50204.9162.013.6108.440.0170.175.3
0.45182.4208.924.1129.755.1123.273.6
0.10138.9333.257.7171.6103.9−1.0568.8

Table 3.

Variation in exergy metrics with the outlet pressure for a turbine expansion process.

3.3. Expansion in a vortex tube

Figure 7a illustrates a counter flow vortex tube [12]. High pressure gas enters the tube through a tangential nozzle (point 1). Colder low-pressure gas leaves via an orifice near the centerline adjacent to the plane of the nozzle (point 2), and warmer low-pressure gas leaves near the periphery at the end of the tube opposite to the nozzle (point 3). The vortex tube requires no work or heat interaction with the surroundings to operate. The cold mass fraction is μ; the hot gas mass fraction is (1 − μ). The exergy balance around the vortex tube is:

e1=μe2+1μe3+dE20

Figure 7.

A vortex tube (a) and the presentation of the expansion process on an exergy-enthalpy diagram (b).

The expansion processes taking place within a vortex tube are presented on an e-h diagram (Figure 7b). The cold stream expands across T0, the hot expands at T > T0. By applying Eqs. (9a) and (9c) the transiting exergies may be determined for each mass stream, cold (1–2) and hot (1–3).

etrcold=eP2T0E21
etrhot=eP3T1E22

As a result, the exergy produced and consumed within the cold and hot streams are:

ΔĖC=ṁμeP2T2e(P2T0)=ṁμΔeTP2ΔĖH=ṁ1μeP3T3e(P3T1)=ṁ1μΔeTP3E23
ĖC=ṁμeP1T1e(P2T0)=ṁμeP,TĖH=ṁ1μeP1T1e(P3T1)=ṁ1μePT1E24

Thus ΔĖCand ΔĖHrepresent the increase in the thermal exergy component due to the cooling of the cold stream and the heating for the hot stream, under conditions of the outlet pressures for each stream. ∇ĖCrepresents the decrease in thermo-mechanical exergy of the cold stream due to the partial thermal exergy destruction because of the temperature drop from T1 to T0, and the decrease of mechanical exergy because of pressure drop from P1 to P3. ∇ĖHis the decrease of mechanical exergy of the hot stream at conditions of constant inlet temperature. The ratio (ΔĖC+ ΔĖH)/ (∇ĖC+ ∇ĖH) gives the value of ηtr.

Example 4

An adiabatic vortex tube is supplied with air as ideal gas at the rate ṁ= 1 kg/s and at P1 = 0.8 MPa, T1 = 308 K. The air expands at the cold end to pressure P2 = 0.1 MPa and at the hot end to the pressure P3 = 0.15 MPa. The ambient temperature T0 = 298 K. Calculate the variation of Ėtr, ΔĖand ∇Ėand ηtr as a function of the cold mass fraction μ in the range 0.2–0.9.

Solution

The results are shown in Table 4. It is illustrated that Ėtr,Hdecreases with the cold mass fraction increase. The Ėtr,Cis zero, because it is defined by ambient conditions P2 = P0 and T2 = T0. As a result, for the cold stream ΔĖCdecreases but ∇ĖCincreases strongly with μ. An opposite effect is observed for the hot stream, where ΔĖHincreases and ∇ĖHdecreases. As a result, ηtr increases, despite the rise in the exergy losses with the increasing cold mass fraction. This can be explained by the fact that the rise in exergy produced in the hot stream surpasses the increase in exergy losses. The exergy efficiency of the vortex tube is relatively low.

μ
(–)
T2
(K)
T3
(K)
ĖC
(kW)
ΔĖC
(kW)
Ėtr,C
(kW)
ĖH
(kW)
ΔĖH
(kW)
Ėtr,H
(kW)
Ḋ
(kW)
ηtr
(%)
0.35268.0329.561.90.60.093.10.921.9153.50.97
0.60273.0360.4106.20.70.057.32.313.5160.51.83
0.75278.0397.6132.70.50.035.83.48.4164.62.32

Table 4.

Variation in exergy metrics with the cold mass fraction for a vortex tube expansion process.

3.4. Compression across ambient temperature

In most refrigeration plants and heat pumps compression starts at T < T0 and ends at T > T0. The process is presented on an e-h diagram (see Figure 8). According to Eq. (9c), transiting exergy is:

etr=eP1T0E25

Figure 8.

Compression process across ambient temperature (T0) on an exergy-enthalpy diagram.

The produced and consumed exergies are:

ΔĖ=ṁeP2T2e(P1T0)=ṁΔeP,TE26
Ė+ẆC=ṁeP1T1e(P1T0)+ẆC=ṁeTP1+ẆCE27

ΔĖrepresents the increase of thermo-mechanical exergy due to the rise in pressure from P to P2 and the rise in temperature from T0 to T2. ∇Ėrepresents the destruction of thermal exergy due to the rise in temperature from T1 to T0 under conditions of constant pressure P1, plus the consumed power ẆC. The ratio ΔĖ/(∇Ė+ẆC)gives the value of exergy efficiency ηtr.

Example 5

An adiabatic compressor of a refrigeration plant is supplied with the working fluid R152a at the rate ṁ= 1 kg/s at P1 = 142.9 kPa and T1 = 263 K (superheated). The fluid is compressed to a pressure of P2 = 615.1 kPa. The ambient temperature T0 = 298 K. Calculate the variation of Ėtr, ΔĖand ∇Ėand ηtr as a function of the isentropic efficiency ηC in the range 0.75–0.90.

Solution

The results are shown in Table 5. The transiting exergy does not change with the isentropic efficiency ηC, because is a function of constant parameters T0 and P1. The exergy consumed does not change either. The produced exergy decreases. This drop in ΔĖis explained by the reduction in “compression reheat”. The decrease in ΔĖis offset by the greater decrease in ẆC, and as a result ηtr increases.

ηC
(–)
ẆC
(kW)
Ė
(kW)
ΔĖ
(kW)
Ḋ
(kW)
Ėtr
(kW)
ηtr
(kW)
0.7566.02.353.315.012.678.0
0.8061.92.352.911.312.682.4
0.8558.32.352.68.012.686.8
0.9055.02.352.35.012.691.3

Table 5.

Variation in exergy metrics with the isentropic efficiency for a compression process.

3.5. Compression and expansion in a one phase ejector

A combination of the processes of vapor expansion and compression takes place within a one-phase ejector presented in Figure 9a. A primary (pr) stream at high pressure P1 and temperature T1 expands and entrains a secondary stream (s) at low pressure P2 and temperature T2 < T0. The ratio ṁs/ṁprgives the value of the entrainment ratio (ω) of the ejector. The mixed stream with the parameters P2 < P3 < P1 and T2 < T3 < T1 leaves the ejector. The exergy balance around the ejector is:

11+ωe1+ω1+ωe2=e3+dE28

Figure 9.

One phase ejector (a) and presentation of expansion and the compression processes (b) on an exergy-enthalpy diagram.

The processes of expansion of the primary stream and compression of the secondary stream are presented on an e-h diagram (Figure 9b). The secondary stream is compressed across T0, meaning that Eq. (9c) is applied to calculate (etr)s. As a result, the transiting exergy for secondary and primary streams are:

etrs=eP2T0E29
etrpr=eP3T3E30

This means that the exergies produced and consumed may be computed as:

ΔĖs=ṁseP3T3e(P2T0)=ṁsΔeP,TsE31
Ės=ṁseP2T2e(P2T0)=ṁseTP2sĖpr=ṁpreP1T1e(P3T3)=ṁpreP,TprE32

ΔĖsis the increase of thermo-mechanical exergy of the secondary stream due to the compression from P2 to P3 and the rise in temperature from T0 to T3. The exergy consumed ∇Ėswithin the secondary stream represents the decrease of thermal exergy component because of the temperature rise from T2 to T0 (the partial cold destruction). The exergy consumed within the primary stream ∇Ėpris the decrease of thermo-mechanical exergy The ratio ΔĖs/(∇Ės+ ∇Ėpr) gives the value of exergy efficiency ηtr. The detailed analysis of efficiencies for different parts of an ejector is given in [13].

Example 6

An ejector of a refrigeration plant is supplied with the working fluid R141b. The parameters of the secondary stream are: P2 = 22.3 kPa, T2 = 268 K. The pressure of the mixed stream is P3 = 91 kPa. The ambient temperature T0 = 289 K. Calculate the variation of (Ėtr)pr, (Ėtr)s, ΔĖand ∇Ėand ηtr as a function of the entrainment ratio ω = ṁs/ṁprin the range 0.15–0.25.

Solution

The calculation results are shown in Table 6. The transiting exergy in the secondary flow is negative because the parameters P2 and T0 define the state of the flow under vacuum conditions. The exergy produced and exergy consumed increase with the entrainment factor. The increase in ΔĖsoffsets the increase in (∇Ės+ ∇Ėpr), and as a result ηtr increases.

ω
(–)
Ėpr
(kW)
Ės
(kW)
ΔĖs
(kW)
Ḋ
(kW)
Ėtr,pr
(kW)
Ėtr,s
(kW)
Ėtr
(kW)
ηtr
(%)
P1
(kPa)
T1
(K)
0.159.990.0171.1898.8184.286−0.5463.74011.91000418
0.1710.070.0191.3348.7554.205−0.6193.58613.21000418
0.2010.190.0231.5478.6664.090−0.7293.36115.21000418
0.2310.290.0261.7548.5623.983−0.8383.14517.01000418
0.2510.360.0281.8908.4983.915−0.9113.00418.21000418

Table 6.

Variation in exergy metrics with the entrainment factor for compression-expansion processes in an ejector.

4. Environmental life cycle analysis and exergy efficiency of cooling systems

Life Cycle Analysis (LCA) is an important tool to analyze environmental problems associated with the production, use, and disposal of products or systems [14]. For every product produced within a system the total inflow and outflow of energy and materials are evaluated. The environmental burdens are associated by quantifying the energy and materials used, as well as the wastes released into the environment. The impact of these uses and releases on the environment is assessed. The multidimensional approach of LCA causes some problems when different substances need to be compared and general agreement is required. This problem may be avoided if exergy is used as a common quantity as proposed by Life Cycle Exergy Analysis [15]. The crucial idea behind this method is the distinction between renewable and non-renewable resources. In order to illustrate the method, let us consider three defined time periods within the life cycle of an ejector refrigeration system driven by solar energy [16]. At first, exergy is required during the construction stage to build the plant and put it into operation. During this period the spent exergy is stored in materials, such as metals, glass etc. For the second period, maintenance required for the system’s operation takes place. Exergy necessary for this maintenance is evaluated. The third period is the clean-up stage, including the plant demolition and the recycling of materials. Exergy used for the clean-up is assessed. The exergy used for the construction, maintenance, and clean-up is assumed to originate from non-renewable resources and is named indirect exergy, Ėind. When the ejector refrigeration system driven by solar energy is put into operation, it starts to deliver a product (cold in this case) with exergy, Ėpr. By considering renewable resources (solar in this case) as free, there will be a net exergy output from the plant until the plant is decommissioned. By considering the total life cycle of the plant the net produced exergy becomes Ėnet= ĖprĖind. The higher this value is for the three time periods defined above, the more sustainable the system is, because the input of non-renewable resources will be paid back during the system’s lifetime. The rise in exergy efficiency of an ejector calculated according to Eqs. (31) and (32) leads to an increase in efficiency of the solar driven refrigeration system [16]. This in turn means that the net produced exergy Ėnetincreases too. Thus, the evaluation of ηtr of an ejector, as presented in Section 3.5, and its subsequent maximization, may lead to the construction and operation of more sustainable solar driven refrigeration plants.

5. Conclusion

The common feature of expansion processes operating below or across ambient temperature is the partial transformation of the mechanical exergy component into the thermal exergy component. Sub-ambient compression processes are characterized by the transformation of work into the mechanical exergy component and the partial destruction of the thermal exergy component below T0. In order to evaluate the efficiency of these transformations the calculations of the variation in mechanical and thermal exergy components are required. These calculations may be done in many different ways, for example the variation in eP depends on the chosen temperature conditions, while the variation in eT depends on the chosen pressure conditions. This multiplicity in the exergy variation evaluation leads to ambiguity in the exergy efficiency definition. The approach based on the exclusion of the “transiting flow” from thermo-mechanical inlet and outlet exergies of an analyzed process overcomes this difficulty. This improvement is possible because the transiting exergy is uniquely defined by a specific combination of the process intensive parameters, namely the inlet and outlet pressures and temperatures, as well as T0. The transiting exergy approach allows non-ambiguous evaluation of two thermodynamic metrics: exergy produced and exergy consumed. Their ratio represents the exergy efficiency; the difference between exergy consumed and exergy produced equals the exergy losses within the process. The phenomenological significance of the transiting exergy and the way in which it can be computed for processes below and across T0 has been illustrated for the cases of an expansion valve, a cryo-expander, a vortex tube, an adiabatic compressor, and a monophasic ejector. The input-output exergy efficiency is not an appropriate criterion for evaluation of these processes.

Acknowledgments

This project is a part of the Collaborative Research and Development (CRD) Grants Program at “Université de Sherbrooke”. The authors acknowledge the support of the Natural Sciences and Engineering Research Council of Canada, Hydro Québec, Rio Tinto Alcan and CanmetENERGY Research Center of Natural Resources Canada (RDCPJ451917-13).

Nomenclature

D ̇Destroyed exergy, (kW)
dSpecific exergy losses, (kJ/kg)
eSpecific exergy, (kJ/kg)
E ̇Exergy, (kW)
hSpecific enthalpy, (kJ/kg)
H ̇Enthalpy, (kW)
(Total) Mass flowrate, (kg/s)
PPressure, (MPa, kPa)
Q ̇Heat rate, (kW)
sSpecific entropy, (kJ/kg K)
TTemperature, (K, °C)
W ̇Mechanical power, (kW)
ηEfficiency, (%)
Consumption
ΔProduction
μCold mass fraction, μ = ṁC/ṁ
ωEntrainment ratio
0Ambient state
1, 2, 3…States in a process
CCold, Compressor
fFuel
HHot
inInlet
indIndirect
intInternal
maxMaximal
minMinimal
outOutlet
prPrimary, Product
S,sSecondary
subCSubcooling
trTransiting

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Mikhail Sorin and Mohammed Khennich (February 20th 2018). Exergy Flows Inside Expansion and Compression Devices Operating below and across Ambient Temperature, Energy Systems and Environment, Pavel Tsvetkov, IntechOpen, DOI: 10.5772/intechopen.74041. Available from:

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