Unformatted text preview: CHAPTER 2 THERMODYNAMICS AND REFRIGERATION CYCLES
THERMODYNAMICS ................................................................ 2.1 Stored Energy .............................................................................. 2.1 Energy in Transition .................................................................... 2.1 First Law of Thermodynamics ................................................... 2.2 Second Law of Thermodynamics ............................................... 2.2 Thermodynamic Analysis of Refrigeration Cycles ..................... 2.3 Equations of State ...................................................................... 2.3 Calculating Thermodynamic Properties .................................... 2.4 COMPRESSION REFRIGERATION CYCLES .......................... 2.6 Carnot Cycle .............................................................................. 2.6 Theoretical SingleStage Cycle Using a Pure Refrigerant or Azeotropic Mixture............................................................. 2.7 Lorenz Refrigeration Cycle ........................................................ 2.8 Theoretical SingleStage Cycle Using Zeotropic Refrigerant Mixture ................................................................ 2.9 Multistage Vapor Compression Refrigeration Cycles .............. 2.10 Actual Refrigeration Systems ................................................... 2.11 ABSORPTION REFRIGERATION CYCLES ........................... 2.13 Ideal Thermal Cycle ................................................................. 2.13 Working Fluid Phase Change Constraints ............................... 2.13 Working Fluids ......................................................................... 2.14 Absorption Cycle Representations ........................................... 2.15 Conceptualizing the Cycle ....................................................... 2.15 Absorption Cycle Modeling ..................................................... 2.16 Ammonia/Water Absorption Cycles ......................................... 2.18 Symbols .................................................................................... 2.19 HERMODYNAMICS is the study of energy, its transformations, and its relation to states of matter. This chapter covers the application of thermodynamics to refrigeration cycles. The first part reviews the first and second laws of thermodynamics and presents methods for calculating thermodynamic properties. The second and third parts address compression and absorption refrigeration cycles, two common methods of thermal energy transfer. T Nuclear (atomic) energy derives from the cohesive forces holding protons and neutrons together as the atom’s nucleus. ENERGY IN TRANSITION
Heat Q is the mechanism that transfers energy across the boundaries of systems with differing temperatures, always toward the lower temperature. Heat is positive when energy is added to the system (see Figure 1). Work is the mechanism that transfers energy across the boundaries of systems with differing pressures (or force of any kind), always toward the lower pressure. If the total effect produced in the system can be reduced to the raising of a weight, then nothing but work has crossed the boundary. Work is positive when energy is removed from the system (see Figure 1). Mechanical or shaft work W is the energy delivered or absorbed by a mechanism, such as a turbine, air compressor, or internal combustion engine. Flow work is energy carried into or transmitted across the system boundary because a pumping process occurs somewhere outside the system, causing fluid to enter the system. It can be more easily understood as the work done by the fluid just outside the system on the adjacent fluid entering the system to force or push it into the system. Flow work also occurs as fluid leaves the system. Flow work (per unit mass) = pv (3) THERMODYNAMICS
A thermodynamic system is a region in space or a quantity of matter bounded by a closed surface. The surroundings include everything external to the system, and the system is separated from the surroundings by the system boundaries. These boundaries can be movable or fixed, real or imaginary. Entropy and energy are important in any thermodynamic system. Entropy measures the molecular disorder of a system. The more mixed a system, the greater its entropy; an orderly or unmixed configuration is one of low entropy. Energy has the capacity for producing an effect and can be categorized into either stored or transient forms. STORED ENERGY
Thermal (internal) energy is caused by the motion of molecules and/or intermolecular forces. Potential energy (PE) is caused by attractive forces existing between molecules, or the elevation of the system. PE = mgz where
m = mass g = local acceleration of gravity z = elevation above horizontal reference plane (1) where p is the pressure and v is the specific volume, or the volume displaced per unit mass evaluated at the inlet or exit. A property of a system is any observable characteristic of the system. The state of a system is defined by specifying the minimum Fig. 1 Energy Flows in General Thermodynamic System Kinetic energy (KE) is the energy caused by the velocity of molecules and is expressed as KE = mV 2/2 (2) where V is the velocity of a fluid stream crossing the system boundary. Chemical energy is caused by the arrangement of atoms composing the molecules.
The preparation of the first and second parts of this chapter is assigned to TC 1.1, Thermodynamics and Psychrometrics. The third part is assigned to TC 8.3, Absorption and HeatOperated Machines. Fig. 1 Energy Flows in General Thermodynamic System 2.1 2.2
set of independent properties. The most common thermodynamic properties are temperature T, pressure p, and specific volume v or density . Additional thermodynamic properties include entropy, stored forms of energy, and enthalpy. Frequently, thermodynamic properties combine to form other properties. Enthalpy h is an important property that includes internal energy and flow work and is defined as h u + pv (4) 2009 ASHRAE Handbook—Fundamentals
2 Vm in u + pv +  + gz 2 2 in – Vm out u + pv +  + gz 2 o ut +Q–W (5) V2 V2 = mf u +  + gz – m i u +  + gz 2 2 f i system where u is the internal energy per unit mass. Each property in a given state has only one definite value, and any property always has the same value for a given state, regardless of how the substance arrived at that state. A process is a change in state that can be defined as any change in the properties of a system. A process is described by specifying the initial and final equilibrium states, the path (if identifiable), and the interactions that take place across system boundaries during the process. A cycle is a process or a series of processes wherein the initial and final states of the system are identical. Therefore, at the conclusion of a cycle, all the properties have the same value they had at the beginning. Refrigerant circulating in a closed system undergoes a cycle. A pure substance has a homogeneous and invariable chemical composition. It can exist in more than one phase, but the chemical composition is the same in all phases. If a substance is liquid at the saturation temperature and pressure, it is called a saturated liquid. If the temperature of the liquid is lower than the saturation temperature for the existing pressure, it is called either a subcooled liquid (the temperature is lower than the saturation temperature for the given pressure) or a compressed liquid (the pressure is greater than the saturation pressure for the given temperature). When a substance exists as part liquid and part vapor at the saturation temperature, its quality is defined as the ratio of the mass of vapor to the total mass. Quality has meaning only when the substance is saturated (i.e., at saturation pressure and temperature). Pressure and temperature of saturated substances are not independent properties. If a substance exists as a vapor at saturation temperature and pressure, it is called a saturated vapor. (Sometimes the term dry saturated vapor is used to emphasize that the quality is 100%.) When the vapor is at a temperature greater than the saturation temperature, it is a superheated vapor. Pressure and temperature of a superheated vapor are independent properties, because the temperature can increase while pressure remains constant. Gases such as air at room temperature and pressure are highly superheated vapors. where subscripts i and f refer to the initial and final states, respectively. Nearly all important engineering processes are commonly modeled as steadyflow processes. Steady flow signifies that all quantities associated with the system do not vary with time. Consequently, V2 · m h +  + gz 2 all streams
entering – 2 V· · · m h +  + gz + Q – W = 0 2 all streams leaving (6) where h = u + pv as described in Equation (4). A second common application is the closed stationary system for which the first law equation reduces to Q – W = [m(uf – ui)]system (7) SECOND LAW OF THERMODYNAMICS
The second law of thermodynamics differentiates and quantifies processes that only proceed in a certain direction (irreversible) from those that are reversible. The second law may be described in several ways. One method uses the concept of entropy flow in an open system and the irreversibility associated with the process. The concept of irreversibility provides added insight into the operation of cycles. For example, the larger the irreversibility in a refrigeration cycle operating with a given refrigeration load between two fixed temperature levels, the larger the amount of work required to operate the cycle. Irreversibilities include pressure drops in lines and heat exchangers, heat transfer between fluids of different temperature, and mechanical friction. Reducing total irreversibility in a cycle improves cycle performance. In the limit of no irreversibilities, a cycle attains its maximum ideal efficiency. In an open system, the second law of thermodynamics can be described in terms of entropy as Q dS system =  + m i s i – m e s e + dI T where
dSsystem m i si me se Q/T total change within system in time dt during process entropy increase caused by mass entering (incoming) entropy decrease caused by mass leaving (exiting) entropy change caused by reversible heat transfer between system and surroundings at temperature T dI = entropy caused by irreversibilities (always positive) = = = = (8) FIRST LAW OF THERMODYNAMICS
The first law of thermodynamics is often called the law of conservation of energy. The following form of the firstlaw equation is valid only in the absence of a nuclear or chemical reaction. Based on the first law or the law of conservation of energy, for any system, open or closed, there is an energy balance as Net amount of energy = Net increase of stored added to system energy in system or [Energy in] – [Energy out] = [Increase of stored energy in system] Figure 1 illustrates energy flows into and out of a thermodynamic system. For the general case of multiple mass flows with uniform properties in and out of the system, the energy balance can be written Equation (8) accounts for all entropy changes in the system. Rearranged, this equation becomes Q = T [( me se – mi si) + dSsys – dI ] (9) In integrated form, if inlet and outlet properties, mass flow, and interactions with the surroundings do not vary with time, the general equation for the second law is Sf – Si
s ystem = rev Q  + T ms in – ms o ut +I (10) Thermodynamics and Refrigeration Cycles
In many applications, the process can be considered to operate steadily with no change in time. The change in entropy of the system is therefore zero. The irreversibility rate, which is the rate of entropy production caused by irreversibilities in the process, can be determined by rearranging Equation (10): · I= · ms
o ut 2.3
Applying the second law to an entire refrigeration cycle shows that a completely reversible cycle operating under the same conditions has the maximum possible COP. Departure of the actual cycle from an ideal reversible cycle is given by the refrigerating efficiency:
R – · ms in – · Q T surr (11) COP = COP r ev (17) Equation (6) can be used to replace the heat transfer quantity. Note that the absolute temperature of the surroundings with which the system is exchanging heat is used in the last term. If the temperature of the surroundings is equal to the system temperature, heat is transferred reversibly and the last term in Equation (11) equals zero. Equation (11) is commonly applied to a system with one mass flow in, the same mass flow out, no work, and negligible kinetic or potential energy flows. Combining Equations (6) and (11) yields h out – h in · · I = m s out – s in – T surr (12) The Carnot cycle usually serves as the ideal reversible refrigeration cycle. For multistage cycles, each stage is described by a reversible cycle. EQUATIONS OF STATE
The equation of state of a pure substance is a mathematical relation between pressure, specific volume, and temperature. When the system is in thermodynamic equilibrium, f ( p, v, T ) = 0 (18) The principles of statistical mechanics are used to (1) explore the fundamental properties of matter, (2) predict an equation of state based on the statistical nature of a particular system, or (3) propose a functional form for an equation of state with unknown parameters that are determined by measuring thermodynamic properties of a substance. A fundamental equation with this basis is the virial equation, which is expressed as an expansion in pressure p or in reciprocal values of volume per unit mass v as pv 2 3  = 1 + B p + C p + D p + RT pv 2 3  = 1 + B v + C v + D v + RT (19) (20) In a cycle, the reduction of work produced by a power cycle (or the increase in work required by a refrigeration cycle) equals the absolute ambient temperature multiplied by the sum of irreversibilities in all processes in the cycle. Thus, the difference in reversible and actual work for any refrigeration cycle, theoretical or real, operating under the same conditions, becomes · · Wactual = Wreversible + T 0 · I (13) THERMODYNAMIC ANALYSIS OF REFRIGERATION CYCLES
Refrigeration cycles transfer thermal energy from a region of low temperature TR to one of higher temperature. Usually the highertemperature heat sink is the ambient air or cooling water, at temperature T0 , the temperature of the surroundings. The first and second laws of thermodynamics can be applied to individual components to determine mass and energy balances and the irreversibility of the components. This procedure is illustrated in later sections in this chapter. Performance of a refrigeration cycle is usually described by a coefficient of performance (COP), defined as the benefit of the cycle (amount of heat removed) divided by the required energy input to operate the cycle: COP Useful refrigerating effect Net energy supplied from external sources (14) where coefficients B', C', D', etc., and B, C, D, etc., are the virial coefficients. B' and B are the second virial coefficients; C' and C are the third virial coefficients, etc. The virial coefficients are functions of temperature only, and values of the respective coefficients in Equations (19) and (20) are related. For example, B' = B/RT and C' = (C – B2)/(RT ) 2. The universal gas constant R is defined as pv T R = lim p 0T (21) For a mechanical vapor compression system, the net energy supplied is usually in the form of work, mechanical or electrical, and may include work to the compressor and fans or pumps. Thus, Q evap COP = W net (15) where pv T is the product of the pressure and the molar specific volume along an isotherm with absolute temperature T. The current best value of R is 1545.32 ft·lbf /(lb mol·°R). The gas constant R is equal to the universal gas constant R divided by the molecular weight M of the gas or gas mixture. The quantity pv/RT is also called the compressibility factor Z, or Z = 1 + (B/v) + (C/v2) + (D/v3) + … (22) In an absorption refrigeration cycle, the net energy supplied is usually in the form of heat into the generator and work into the pumps and fans, or Q evap COP = Q gen + W net (16) In many cases, work supplied to an absorption system is very small compared to the amount of heat supplied to the generator, so the work term is often neglected. An advantage of the virial form is that statistical mechanics can be used to predict the lowerorder coefficients and provide physical significance to the virial coefficients. For example, in Equation (22), the term B/v is a function of interactions between two molecules, C/v 2 between three molecules, etc. Because lowerorder interactions are common, contributions of the higherorder terms are successively less. Thermodynamicists use the partition or distribution function to determine virial coefficients; however, experimental values of the second and third coefficients are preferred. For dense fluids, many higherorder terms are necessary that can neither be satisfactorily predicted from theory nor determined from experimental measurements. In general, a truncated virial expansion of four terms is valid for densities of less than onehalf the value at the critical 2.4
point. For higher densities, additional terms can be used and determined empirically. Computers allow the use of very complex equations of state in calculating pvT values, even to high densities. The BenedictWebbRubin (BWR) equation of state (Benedict et al. 1940) and MartinHou equation (1955) have had considerable use, but should generally be limited to densities less than the critical value. Strobridge (1962) suggested a modified BenedictWebbRubin relation that gives excellent results at higher densities and can be used for a pvT surface that extends into the liquid phase. The BWR equation has been used extensively for hydrocarbons (Cooper and Goldfrank 1967): P = RT v + B o RT – A o – C o T +a v + c 1+
6 2 v
2 2009 ASHRAE Handbook—Fundamentals
corresponding states provides useful approximations, and numerous modifications have been reported. More complex treatments for predicting properties, which recognize similarity of fluid properties, are by generalized equations of state. These equations ordinarily allow adjustment of the pvT surface by introducing parameters. One example (Hirschfelder et al. 1958) allows for departures from the principle of corresponding states by adding two correlating parameters. CALCULATING THERMODYNAMIC PROPERTIES
Although equations of state provide pvT relations, thermodynamic analysis usually requires values for internal energy, enthalpy, and entropy. These properties have been tabulated for many substances, including refrigerants (see Chapters 1, 30, and 33), and can be extracted from such tables by interpolating manually or with a suitable computer program. This approach is appropriate for hand calculations and for relatively simple computer models; however, for many computer simulations, the overhead in memory or input and output required to use tabulated data can make this approach unacceptable. For large thermal system simulations or complex analyses, it may be more efficient to determine internal energy, enthalpy, and entropy using fundamental thermodynamic relations or curves fit to experimental data. Some of these relations are discussed in the following sections. Also, the thermodynamic relations discussed in those sections are the basis for constructing tables of thermodynamic property data. Further information on the topic may be found in references covering system modeling and thermodynamics (Howell and Buckius 1992; Stoecker 1989). At least two intensive properties (properties independent of the quantity of substance, such as temperature, pressure, specific volume, and specific enthalpy) must be known to determine the remaining properties. If two known properties are either p, v, or T (these are relatively easy to measure and are commonly used in simulations), the third can be determined throughout the range of interest using an equation of state. Furthermore, if the specific heats at zero pressure are known, specific heat can be accurately determined from spectroscopic measurements using statistical mechanics (NASA 1971). Entropy may be considered a function of T and p, and from calculus an infinitesimal change in entropy can be written as s s ds =  dT + Tp p dp
T v + b RT – a vT
3 2 2 v 3 ve 2 – (23) where the constant coefficients are Ao, Bo, Co, a, b, c, , and . The MartinHou equation, developed for fluorinated hydrocarbon properties, has been used to calculate the thermodynamic property tables in Chapter 30 and in ASHRAE Thermodynamic Properties of Refrigerants (Stewart et al. 1986). The MartinHou equation is A3 + B3 T + C3 e RT A 2 + B 2 T + C 2 e p =  +  + 2 3 v–b v–b v–b A4 + B4 T A5 + B5 T + C5 e av +  +  + A 6 + B 6 T e (24) 4 5 v–b v–b where the constant coefficients are Ai , Bi , Ci , k, b, and a. Strobridge (1962) suggested an equation of state that was developed for nitrogen properties and used for most cryogenic fluids. This equation combines the BWR equation of state with an equation for highdensity nitrogen suggested by Benedict (1937). These equations have been used successfully for liquid and vapor phases, extending in the liquid phase to the triplepoint temperature and the freezing line, and in the vapor phase from 18 to 1800°R, with pressures to 150,000 psi. The Strobridge equation is accurate within the uncertainty of the measured pvT data: n3 n4 n5 p = RT + R n 1 T + n 2 +  +  + T T2 T4 + Rn 6 T + n 7 +
3 3 2 – kT T c – kT T c – kT T c (26) + n8 T 4 Likewise, a change in enthalpy can be written as
2 n 9 n 10 n 11  +  +  exp – n 16 T 2 T3 T 4 n 12 n 13 n 14  +  +  exp – n 16 T2 T3 T4 h h dh =  dT + Tp p + n 15
6 dp
T (27) + 5 2 (25) Using the Gibbs relation Tds dh – vdp and the definition of specific heat at constant pressure, cp ( h / T )p , Equation (27) can be rearranged to yield cp ds =  dT + T h p dp – v T T (28) The 15 coefficients of this equation’s linear terms are determined by a leastsquare fit to experimental data. Hust and McCarty (1967) and Hust and Stewart (1966) give further information on methods and techniques for determining equations of state. In the absence of experimental data, Van der Waals’ principle of corresponding states can predict fluid properties. This principle relates properties of similar substances by suitable reducing factors (i.e., the pvT surfaces of similar fluids in a given region are assumed to be of similar shape). The critical point can be used to define reducing parameters to scale the surface of one fluid to the dimensions of another. Modifications of this principle, as suggested by Kamerlingh Onnes, a Dutch cryogenic researcher, have been used to improve correspondence at low pressures. The principle of Equations (26) and (28) combine to yield ( s/ T )p = cp /T. Then, using the Maxwell relation ( s/ p)T = –( v/ T )p , Equation (26) may be rewritten as cp v ds =  dT –  dp Tp T This is an expression for an exact derivative, so it follows that (29) Thermodynamics and Refrigeration Cycles
cp = –T pT
2 2.5
If vapor pressure and liquid and vapor density data (all relatively easy measurements to obtain) are known at saturation, then changes in enthalpy and entropy can be calculated using Equation (37). v
2 p (30) T Integrating this expression at a fixed temperature yields
p 2 Phase Equilibria for Multicomponent Systems
(31) To understand phase equilibria, consider a container full of a liquid made of two components; the more volatile component is designated i and the less volatile component j (Figure 2A). This mixture is all liquid because the temperature is low (but not so low that a solid appears). Heat added at a constant pressure raises the mixture’s temperature, and a sufficient increase causes vapor to form, as shown in Figure 2B. If heat at constant pressure continues to be added, eventually the temperature becomes so high that only vapor remains in the container (Figure 2C). A temperatureconcentration (T x) diagram is useful for exploring details of this situation. Figure 3 is a typical T x diagram valid at a fixed pressure. The case shown in Figure 2A, a container full of liquid mixture with mole fraction xi,0 at temperature T0 , is point 0 on the T x diagram. When heat is added, the temperature of the mixture increases. The point at which vapor begins to form is the bubble point. Starting at point 0, the first bubble forms at temperature T1 (point 1 on the diagram). The locus of bubble points is the bubblepoint curve, which provides bubble points for various liquid mole fractions xi. Fig. 2 Mixture of i and j Components in Constant Pressure Container (34) cp = cp 0 – T
0 v
2 T dp T where cp 0 is the known zeropressure specific heat, and dpT is used to indicate that integration is performed at a fixed temperature. The second partial derivative of specific volume with respect to temperature can be determined from the equation of state. Thus, Equation (31) can be used to determine the specific heat at any pressure. Using Tds dh – vdp, Equation (29) can be written as dh = c p dT + v – T v T dp
p (32) Equations (28) and (32) may be integrated at constant pressure to obtain
T1 s T1 , p0 = s T0 , p0 +
T0 T1 cp  dTp T (33) and h T1 , p0 = h T0 , p0 +
T0 c p dT Integrating the Maxwell relation ( s/ p)T = – ( v/ T )p gives an equation for entropy changes at a constant temperature as
p1 s T0 , p 1 = s T0 , p 0 –
p0 v dp Tp T (35) Likewise, integrating Equation (32) along an isotherm yields the following equation for enthalpy changes at a constant temperature:
p1 Fig. 2 Mixture of i and j Components in ConstantPressure Container h T0 , p1 = h T0 , p 0 +
p0 v–T v dp Tp (36) Fig. 3 TemperatureConcentration (Tx) Diagram for Zeotropic Mixture Internal energy can be calculated from u = h – pv. When entropy or enthalpy are known at a reference temperature T0 and pressure p0, values at any temperature and pressure may be obtained by combining Equations (33) and (35) or Equations (34) and (36). Combinations (or variations) of Equations (33) through (36) can be incorporated directly into computer subroutines to calculate properties with improved accuracy and efficiency. However, these equations are restricted to situations where the equation of state is valid and the properties vary continuously. These restrictions are violated by a change of phase such as evaporation and condensation, which are essential processes in airconditioning and refrigerating devices. Therefore, the Clapeyron equation is of particular value; for evaporation or condensation, it gives dp dT where
sfg = entropy of vaporization hfg = enthalpy of vaporization vfg = specific volume difference between vapor and liquid phases s at h fg s fg =  = v fg Tv fg (37) Fig. 3 TemperatureConcentration (Tx) Diagram for Zeotropic Mixture 2.6
When the first bubble begins to form, the vapor in the bubble may not have the same mole fraction as the liquid mixture. Rather, the mole fraction of the more volatile species is higher in the vapor than in the liquid. Boiling prefers the more volatile species, and the T x diagram shows this behavior. At Tl, the vaporforming bubbles have an i mole fraction of yi,l. If heat continues to be added, this preferential boiling depletes the liquid of species i and the temperature required to continue the process increases. Again, the T x diagram reflects this fact; at point 2 the i mole fraction in the liquid is reduced to xi,2 and the vapor has a mole fraction of yi,2. The temperature required to boil the mixture is increased to T2. Position 2 on the Tx diagram could correspond to the physical situation shown in Figure 2B. If constantpressure heating continues, all the liquid eventually becomes vapor at temperature T3. The vapor at this point is shown as position 3 in Figure 3. At this point the i mole fraction in the vapor yi,3 equals the starting mole fraction in the allliquid mixture xi,1. This equality is required for mass and species conservation. Further addition of heat simply raises the vapor temperature. The final position 4 corresponds to the physical situation shown in Figure 2C. Starting at position 4 in Figure 3, heat removal leads to initial liquid formation when position 3 (the dew point) is reached.The locus of dew points is called the dewpoint curve. Heat removal causes the liquid phase of the mixture to reverse through points 3, 2, 1, and to starting point 0. Because the composition shifts, the temperature required to boil (or condense) this mixture changes as the process proceeds. This is known as temperature glide. This mixture is therefore called zeotropic. Most mixtures have T x diagrams that behave in this fashion, but some have a markedly different feature. If the dewpoint and bubblepoint curves intersect at any point other than at their ends, the mixture exhibits azeotropic behavior at that composition. This case is shown as position a in the T x diagram of Figure 4. If a container of liquid with a mole fraction xa were boiled, vapor would be formed with an identical mole fraction ya . The addition of heat at constant pressure would continue with no shift in composition and no temperature glide. Perfect azeotropic behavior is uncommon, although nearazeotropic behavior is fairly common. The azeotropic composition is pressuredependent, so operating pressures should be considered for their effect on mixture behavior. Azeotropic and nearazeotropic refrigerant mixtures are widely used. The properties of an azeotropic mixture are such that they may be conveniently treated as pure substance properties. Phase equilibria for zeotropic mixtures, however, require special treatment, using an equationofstate approach Fig. 4 Azeotropic Behavior Shown on Tx Diagram 2009 ASHRAE Handbook—Fundamentals
with appropriate mixing rules or using the fugacities with the standard state method (Tassios 1993). Refrigerant and lubricant blends are a zeotropic mixture and can be treated by these methods (Martz et al. 1996a, 1996b; Thome 1995). COMPRESSION REFRIGERATION CYCLES
CARNOT CYCLE
The Carnot cycle, which is completely reversible, is a perfect model for a refrigeration cycle operating between two fixed temperatures, or between two fluids at different temperatures and each with infinite heat capacity. Reversible cycles have two important properties: (1) no refrigerating cycle may have a coefficient of performance higher than that for a reversible cycle operated between the same temperature limits, and (2) all reversible cycles, when operated between the same temperature limits, have the same coefficient of performance. Proof of both statements may be found in almost any textbook on elementary engineering thermodynamics. Figure 5 shows the Carnot cycle on temperatureentropy coordinates. Heat is withdrawn at constant temperature TR from the region to be refrigerated. Heat is rejected at constant ambient temperature T0. The cycle is completed by an isentropic expansion and an isentropic compression. The energy transfers are given by Q0 = T0(S2 – S3) Qi = TR (S1 – S4) = TR (S2 – S3) Wnet = Qo – Qi Thus, by Equation (15), TR COP = T0 – TR (38) Example 1. Determine entropy change, work, and COP for the cycle shown in Figure 6. Temperature of the refrigerated space TR is 400°R, and that of the atmosphere T0 is 500°R. Refrigeration load is 200 Btu. Solution: S = S1 – S4 = Qi/TR = 200/400 = 0.500 Btu/°R W= S(T0 – TR) = 0.5(500 – 400) = 50 Btu COP = Qi /(Qo – Qi) = Qi /W = 200/50 = 4 Flow of energy and its area representation in Figure 6 are Energy Qi Qo W Btu 200 250 50 Area b a+b a Fig. 5 Carnot Refrigeration Cycle Fig. 4 Azeotropic Behavior Shown on Tx Diagram Fig. 5 Carnot Refrigeration Cycle Thermodynamics and Refrigeration Cycles
The net change of entropy of any refrigerant in any cycle is always zero. In Example 1, the change in entropy of the refrigerated space is SR = –200/400 = –0.5 Btu/°R and that of the atmosphere is So = 250/ 500 = 0.5 Btu/°R. The net change in entropy of the isolated system is Stotal = SR + So = 0. 2.7
The net work for the cycle is Wnet = 1Wb + bWc – 3Wd = Area d1bc3d and TR d Q1 COP =  = W net T0 – TR The Carnot cycle in Figure 7 shows a process in which heat is added and rejected at constant pressure in the twophase region of a refrigerant. Saturated liquid at state 3 expands isentropically to the low temperature and pressure of the cycle at state d. Heat is added isothermally and isobarically by evaporating the liquidphase refrigerant from state d to state 1. The cold saturated vapor at state 1 is compressed isentropically to the high temperature in the cycle at state b. However, the pressure at state b is below the saturation pressure corresponding to the high temperature in the cycle. The compression process is completed by an isothermal compression process from state b to state c. The cycle is completed by an isothermal and isobaric heat rejection or condensing process from state c to state 3. Applying the energy equation for a mass of refrigerant m yields (all work and heat transfer are positive)
3Wd 1Wb bWc d Q1 THEORETICAL SINGLESTAGE CYCLE USING A PURE REFRIGERANT OR AZEOTROPIC MIXTURE
A system designed to approach the ideal model shown in Figure 7 is desirable. A pure refrigerant or azeotropic mixture can be used to maintain constant temperature during phase changes by maintaining constant pressure. Because of concerns such as high initial cost and increased maintenance requirements, a practical machine has one compressor instead of two and the expander (engine or turbine) is replaced by a simple expansion valve, which throttles refrigerant from high to low pressure. Figure 8 shows the theoretical singlestage cycle used as a model for actual systems. Applying the energy equation for a mass m of refrigerant yields
4Q1 1W2 2Q3 = m(h3 – hd) = m (hb – h1) = m (h1 – h4) = m (h2 – h1) = m (h2 – h3) h3 = h4 (39a) (39b) (39c) (39d) = T0(Sb – Sc) – m (hb – hc) = m (h1 – hd) = Area defld Fig. 6 TemperatureEntropy Diagram for Carnot Refrigeration Cycle of Example 1 Constantenthalpy throttling assumes no heat transfer or change in potential or kinetic energy through the expansion valve. The coefficient of performance is h1 – h4 4Q 1 COP =  = W2 h2 – h1 1 (40) The theoretical compressor displacement CD (at 100% volumetric efficiency) is · CD = m v 1 (41) Fig. 8 Theoretical SingleStage Vapor Compression Refrigeration Cycle Fig. 6 TemperatureEntropy Diagram for Carnot Refrigeration Cycle of Example 1 Fig. 7 Carnot Vapor Compression Cycle Fig. 7 Carnot Vapor Compression Cycle Fig. 8 Theoretical SingleStage Vapor Compression Refrigeration Cycle 2.8
which is a measure of the physical size or speed of the compressor required to handle the prescribed refrigeration load.
Example 2. A theoretical singlestage cycle using R134a as the refrigerant operates with a condensing temperature of 90°F and an evaporating temperature of 0°F. The system produces 15 tons of refrigeration. Determine the (a) thermodynamic property values at the four main state points of the cycle, (b) COP, (c) cycle refrigerating efficiency, and (d) rate of refrigerant flow. Solution: (a) Figure 9 shows a schematic ph diagram for the problem with numerical property data. Saturated vapor and saturated liquid properties for states 1 and 3 are obtained from the saturation table for R134a in Chapter 30. Properties for superheated vapor at state 2 are obtained by linear interpolation of the superheat tables for R134a in Chapter 30. Specific volume and specific entropy values for state 4 are obtained by determining the quality of the liquidvapor mixture from the enthalpy. h4 – hf 41.645 – 12.207 x 4 =  =  = 0.3237 hg – hf 103.156 – 12.207 v4 = vf + x4(vg – vf ) = 0.01185 + 0.3237(2.1579 – 0.01185) = 0.7065 ft3/lb s4 = sf + x4(sg – sf ) = 0.02771 + 0.3237(0.22557 – 0.02771) = 0.09176 Btu/lb·°R The property data are tabulated in Table 1. (b) By Equation (40), COP = 103.156 – 41.645 = 3.98 118.61 – 103.156 (c) By Equations (17) and (38),
R 2009 ASHRAE Handbook—Fundamentals
and 15 tons 200Btu min ton · m =  = 48.8 lb/min 103.156 – 41.645 Btu/lb The saturation temperatures of the singlestage cycle strongly influence the magnitude of the coefficient of performance. This influence may be readily appreciated by an area analysis on a temperatureentropy (T s) diagram. The area under a reversible process line on a T s diagram is directly proportional to the thermal energy added or removed from the working fluid. This observation follows directly from the definition of entropy [see Equation (8)]. In Figure 10, the area representing Qo is the total area under the constantpressure curve between states 2 and 3. The area representing the refrigerating capacity Qi is the area under the constant pressure line connecting states 4 and 1. The net work required Wnet equals the difference (Qo – Qi), which is represented by the shaded area shown on Figure 10. Because COP = Qi /Wnet , the effect on the COP of changes in evaporating temperature and condensing temperature may be observed. For example, a decrease in evaporating temperature TE significantly increases Wnet and slightly decreases Qi. An increase in condensing temperature TC produces the same results but with less effect on Wnet . Therefore, for maximum coefficient of performance, the cycle should operate at the lowest possible condensing temperature and maximum possible evaporating temperature. LORENZ REFRIGERATION CYCLE
The Carnot refrigeration cycle includes two assumptions that make it impractical. The heat transfer capacities of the two external fluids are assumed to be infinitely large so the external fluid temperatures remain fixed at T0 and TR (they become infinitely large thermal reservoirs). The Carnot cycle also has no thermal resistance between the working refrigerant and external fluids in the two heat exchange processes. As a result, the refrigerant must remain fixed at T0 in the condenser and at TR in the evaporator. The Lorenz cycle eliminates the first restriction in the Carnot cycle by allowing the temperature of the two external fluids to vary during heat exchange. The second assumption of negligible thermal resistance between the working refrigerant and two external fluids remains. Therefore, the refrigerant temperature must change during the two heat exchange processes to equal the changing temperature of the external fluids. This cycle is completely reversible when operating between two fluids that each have a finite but constant heat capacity. COP T 3 – T 1 3.98 90 =  =  = 0.78 or 78% 459.6 T1 (d) The mass flow of refrigerant is obtained from an energy balance on the evaporator. Thus, · · m h 1 – h 4 = Q i = 15 tons Table 1 Thermodynamic Property Data for Example 2
State 1 2 3 4 t , °F 0 104.3 90.0 0 p, psia 21.171 119.01 119.01 21.171 v , ft3/lb 2.1579 0.4189 0.0136 0.7065 h, Btu/lb 103.156 118.61 41.645 41.645 s , Btu/lb °R 0.22557 0.22557 0.08565 0.09176 Fig. 10 Areas on Ts Diagram Representing Refrigerating Effect and Work Supplied for Theoretical SingleStage Cycle Fig. 9 Schematic ph Diagram for Example 2 Fig. 9 Schematic p h Diagram for Example 2 Fig. 10 Areas on T s Diagram Representing Refrigerating Effect and Work Supplied for Theoretical SingleStage Cycle Thermodynamics and Refrigeration Cycles
Figure 11 is a schematic of a Lorenz cycle. Note that this cycle does not operate between two fixed temperature limits. Heat is added to the refrigerant from state 4 to state 1. This process is assumed to be linear on Ts coordinates, which represents a fluid with constant heat capacity. The refrigerant temperature is increased in isentropic compression from state 1 to state 2. Process 23 is a heat rejection process in which the refrigerant temperature decreases linearly with heat transfer. The cycle ends with isentropic expansion between states 3 and 4. The heat addition and heat rejection processes are parallel so the entire cycle is drawn as a parallelogram on T s coordinates. A Carnot refrigeration cycle operating between T0 and TR would lie between states 1, a, 3, and b; the Lorenz cycle has a smaller refrigerating effect and requires more work, but this cycle is a more practical reference when a refrigeration system operates between two singlephase fluids such as air or water. The energy transfers in a Lorenz refrigeration cycle are as follows, where T is the temperature change of the refrigerant during each of the two heat exchange processes. Qo = (T0 + T/2)(S2 – S3) Qi = (TR – T/2)(S1 – S4) = (TR – T/2)(S2 – S3) Wnet = Qo – QR Thus by Equation (15), TR – T 2 COP = T0 – TR + T (42) 2.9
Lorenz cycle. This difference is caused by the finite temperature difference between the working fluid in the cycle compared to the bounding temperature reservoirs. However, as discussed previously, the assumption of constanttemperature heat reservoirs is not necessarily a good representation of an actual refrigeration system because of the temperature changes that occur in the heat exchangers. THEORETICAL SINGLESTAGE CYCLE USING ZEOTROPIC REFRIGERANT MIXTURE
A practical method to approximate the Lorenz refrigeration cycle is to use a fluid mixture as the refrigerant and the four system components shown in Figure 8. When the mixture is not azeotropic and the phase change occurs at constant pressure, the temperatures change during evaporation and condensation and the theoretical singlestage cycle can be shown on Ts coordinates as in Figure 12. In comparison, Figure 10 shows the system operating with a pure simple substance or an azeotropic mixture as the refrigerant. Equations (14), (15), (39), (40), and (41) apply to this cycle and to conventional cycles with constant phase change temperatures. Equation (42) should be used as the reversible cycle COP in Equation (17). For zeotropic mixtures, the concept of constant saturation temperatures does not exist. For example, in the evaporator, the refrigerant enters at T4 and exits at a higher temperature T1. The temperature of saturated liquid at a given pressure is the bubble point and the temperature of saturated vapor at a given pressure is called the dew point. The temperature T3 in Figure 12 is at the bubble point at the condensing pressure and T1 is at the dew point at the evaporating pressure. Areas on a Ts diagram representing additional work and reduced refrigerating effect from a Lorenz cycle operating between the same two temperatures T1 and T3 with the same value for T can be analyzed. The cycle matches the Lorenz cycle most closely when counterflow heat exchangers are used for both the condenser and evaporator. In a cycle that has heat exchangers with finite thermal resistances and finite external fluid capacity rates, Kuehn and Gronseth (1986) showed that a cycle using a refrigerant mixture has a higher coefficient of performance than one using a simple pure substance as a refrigerant. However, the improvement in COP is usually small. Performance of a mixture can be improved further by reducing the heat exchangers’ thermal resistance and passing fluids through them in a counterflow arrangement. Fig. 12 Areas on Ts Diagram Representing Refrigerating Effect and Work Supplied for Theoretical SingleStage Cycle Using Zeotropic Mixture as Refrigerant Example 3. Determine the entropy change, work required, and COP for the Lorenz cycle shown in Figure 11 when the temperature of the refrigerated space is TR = 400°R, ambient temperature is T0 = 500°R, T of the refrigerant is 10°R, and refrigeration load is 200 Btu. Solution:
1 S=
4 Qi Q i =  = 200 = 0.5063 Btu T TR – T 2 395 T2 R Qo = T0 + S = 500 + 5 0.5063 = 255.68 Btu W net = Q o – Q R = 255.68 – 200 = 55.68 Btu TR – T 2 400 – 10 2 395 COP =  =  =  = 3.591 T0 – TR + T 500 – 400 + 10 110 Note that the entropy change for the Lorenz cycle is larger than for the Carnot cycle when both operate between the same two temperature reservoirs and have the same capacity (see Example 1). That is, both the heat rejection and work requirement are larger for the Fig. 11 Processes of Lorenz Refrigeration Cycle Fig. 11 Processes of Lorenz Refrigeration Cycle Fig. 12 Areas on Ts Diagram Representing Refrigerating Effect and Work Supplied for Theoretical SingleStage Cycle Using Zeotropic Mixture as Refrigerant 2.10
MULTISTAGE VAPOR COMPRESSION REFRIGERATION CYCLES
Multistage or multipressure vapor compression refrigeration is used when several evaporators are needed at various temperatures, such as in a supermarket, or when evaporator temperature becomes very low. Low evaporator temperature indicates low evaporator pressure and low refrigerant density into the compressor. Two small compressors in series have a smaller displacement and usually operate more efficiently than one large compressor that covers the entire pressure range from the evaporator to the condenser. This is especially true in ammonia refrigeration systems because of the large amount of superheating that occurs during the compression process. Thermodynamic analysis of multistage cycles is similar to analysis of singlestage cycles, except that mass flow differs through various components of the system. A careful mass balance and energy balance on individual components or groups of components ensures correct application of the first law of thermodynamics. Care must also be used when performing secondlaw calculations. Often, the refrigerating load is comprised of more than one evaporator, so the total system capacity is the sum of the loads from all evaporators. Likewise, the total energy input is the sum of the work into all compressors. For multistage cycles, the expression for the coefficient of performance given in Equation (15) should be written as COP = Q i / W net (43) 2009 ASHRAE Handbook—Fundamentals Fig. 13 Schematic and PressureEnthalpy Diagram for DualCompression, DualExpansion Cycle of Example 4 When compressors are connected in series, the vapor between stages should be cooled to bring the vapor to saturated conditions before proceeding to the next stage of compression. Intercooling usually minimizes the displacement of the compressors, reduces the work requirement, and increases the COP of the cycle. If the refrigerant temperature between stages is above ambient, a simple intercooler that removes heat from the refrigerant can be used. If the temperature is below ambient, which is the usual case, the refrigerant itself must be used to cool the vapor. This is accomplished with a flash intercooler. Figure 13 shows a cycle with a flash intercooler installed. The superheated vapor from compressor I is bubbled through saturated liquid refrigerant at the intermediate pressure of the cycle. Some of this liquid is evaporated when heat is added from the superheated refrigerant. The result is that only saturated vapor at the intermediate pressure is fed to compressor II. A common assumption is to operate the intercooler at about the geometric mean of the evaporating and condensing pressures. This operating point provides the same pressure ratio and nearly equal volumetric efficiencies for the two compressors. Example 4 illustrates the thermodynamic analysis of this cycle.
Example 4. Determine the thermodynamic properties of the eight state points shown in Figure 13, the mass flows, and the COP of this theoretical multistage refrigeration cycle using R134a. The saturated evaporator temperature is 0°F, the saturated condensing temperature is 90°F, and the refrigeration load is 15 tons. The saturation temperature of the refrigerant in the intercooler is 40°F, which is nearly at the geometric mean pressure of the cycle. Solution: Thermodynamic property data are obtained from the saturation and superheat tables for R134a in Chapter 30. States 1, 3, 5, and 7 are obtained directly from the saturation table. State 6 is a mixture of liquid and vapor. The quality is calculated by h6 – h7 41.645 – 24.890 x 6 =  =  = 0.19955 h3 – h7 108.856 – 24.890 Then, v6 = v7 + x6 (v3 – v7) = 0.01252 + 0.19955(0.9528 – 0.01252) = 0.2002 ft3/lb Fig. 13 Schematic and PressureEnthalpy Diagram for DualCompression, DualExpansion Cycle of Example 4 Table 2 Thermodynamic Property Values for Example 4
Temperature, Pressure, °F psia 0.00 49.03 40.00 96.39 90.00 40.00 40.00 0.00 21.171 49.741 49.741 119.01 119.01 49.741 49.741 21.171 Specific Volume, ft3/lb 2.1579 0.9766 0.9528 0.4082 0.01359 0.2002 0.01252 0.3112 Specific Enthalpy, Btu/lb 103.156 110.65 108.856 116.64 41.645 41.645 24.890 24.890 Specific Entropy, Btu/lb·°R 0.22557 0.22557 0.22207 0.22207 0.08565 0.08755 0.05403 0.05531 State 1 2 3 4 5 6 7 8 s6 = s7 + x6 (s3 – s7) = 0.05402 + 0.19955(0.22207 – 0.05402) = 0.08755 Btu/lb·°R Similarly for state 8, x8 = 0.13951, v8 = 0.3112 ft3/lb, s8 = 0.05531 Btu/lb·°R States 2 and 4 are obtained from the superheat tables by linear interpolation. The thermodynamic property data are summarized in Table 2. Mass flow through the lower circuit of the cycle is determined from an energy balance on the evaporator. · Qi 15 tons 200 Btu min ton · m 1 =  =  = 38.33 lb/min h1 – h8 103.156 – 24.890 B tu/lb · · · · m1 = m2 = m7 = m8 For the upper circuit of the cycle, · · · · m3 = m4 = m5 = m6 Thermodynamics and Refrigeration Cycles
Assuming the intercooler has perfect external insulation, an energy bal· ance on it is used to compute m 3 . · · · · m6 h6 + m2 h2 = m7 h7 + m3 h3 · Rearranging and solving for m 3 , 24.890 – 110.65 · · h7 – h2 m 3 = m 2  = 38.33 lb min  = 48.91 lb/min h6 – h3 41.645 – 108.856 · · W I = m 1 h 2 – h 1 = 38.33 lb/min 110.65 – 103.156 Btu lb · W II = 287.2 Btu/min · = m 3 h 4 – h 3 = 48.91 lb/min 116.64 – 108.856 Btu lb State 1 2 3 4 5 6 7 2.11
Solution: The mass flow of refrigerant is the same through all components, so it is only computed once through the evaporator. Each component in the system is analyzed sequentially, beginning with the evaporator. Equation (6) is used to perform a firstlaw energy balance on each component, and Equations (11) and (13) are used for the secondlaw analysis. Note that the temperature used in the secondlaw analysis is the absolute temperature. Table 3 Measured and Computed Thermodynamic Properties of R22 for Example 5
Measured Computed Specific Enthalpy, Btu/lb 106.4 108.1 128.8 124.8 37.4 36.8 36.8 Specific Entropy, Btu/lb·°R 0.2291 0.2330 0.2374 0.2314 0.0761 0.0750 0.0800 Specific Volume, ft3/lb 1.213 1.276 0.331 0.318 0.014 0.014 0.308 = 380.7 Btu/min · Qi 15 tons 200 Btu min ton COP =  =  = 4.49 · ·287.2 + 380.7 Btu/min W I + W II Pressure, Temperature, psia °F 45.0 44.0 210.0 208.0 205.0 204.0 46.5 15.0 25.0 180.0 160.0 94.0 92.0 9.0 Examples 2 and 4 have the same refrigeration load and operate with the same evaporating and condensing temperatures. The twostage cycle in Example 4 has a higher COP and less work input than the singlestage cycle. Also, the highest refrigerant temperature leaving the compressor is about 96°F for the twostage cycle versus about 104°F for the singlestage cycle. These differences are more pronounced for cycles operating at larger pressure ratios. Fig. 14 Schematic of Real, DirectExpansion, SingleStage Mechanical VaporCompression Refrigeration System ACTUAL REFRIGERATION SYSTEMS
Actual systems operating steadily differ from the ideal cycles considered in the previous sections in many respects. Pressure drops occur everywhere in the system except in the compression process. Heat transfers between the refrigerant and its environment in all components. The actual compression process differs substantially from isentropic compression. The working fluid is not a pure substance but a mixture of refrigerant and oil. All of these deviations from a theoretical cycle cause irreversibilities within the system. Each irreversibility requires additional power into the compressor. It is useful to understand how these irreversibilities are distributed throughout a real system; this insight can be useful when design changes are contemplated or operating conditions are modified. Example 5 illustrates how the irreversibilities can be computed in a real system and how they require additional compressor power to overcome. Input data have been rounded off for ease of computation.
Example 5. An aircooled, directexpansion, singlestage mechanical vaporcompression refrigerator uses R22 and operates under steady conditions. A schematic of this system is shown in Figure 14. Pressure drops occur in all piping, and heat gains or losses occur as indicated. Power input includes compressor power and the power required to operate both fans. The following performance data are obtained: Ambient air temperature t0 Refrigerated space temperature tR · Q evap Refrigeration load · W comp Compressor power input · Condenser fan input W CF · Evaporator fan input W EF = = = = = = 90°F 20°F 2 tons 3.0 hp 0.2 hp 0.15 hp Fig. 14 Schematic of Real, DirectExpansion, SingleStage Mechanical VaporCompression Refrigeration System Fig. 15 PressureEnthalpy Diagram of Actual System and Theoretical SingleStage System Operating Between Same Inlet Air Temperatures TR and TO Refrigerant pressures and temperatures are measured at the seven locations shown in Figure 14. Table 3 lists the measured and computed thermodynamic properties of the refrigerant, neglecting the dissolved oil. A pressureenthalpy diagram of this cycle is shown in Figure 15 and is compared with a theoretical singlestage cycle operating between the air temperatures tR and t0. Compute the energy transfers to the refrigerant in each component of the system and determine the secondlaw irreversibility rate in each component. Show that the total irreversibility rate multiplied by the absolute ambient temperature is equal to the difference between the actual power input and the power required by a Carnot cycle operating between tR and t0 with the same refrigerating load. Fig. 15 PressureEnthalpy Diagram of Actual System and Theoretical SingleStage System Operating Between Same Inlet Air Temperatures tR and t0 2.12
Evaporator: Energy balance
7Q1 2009 ASHRAE Handbook—Fundamentals
Table 4 Energy Transfers and Irreversibility Rates for Refrigeration System in Example 5
· = m h 1 – h 7 = 24,000 Btu/h Component Evaporator Suction line Compressor Discharge line Condenser Liquid line Expansion device R Totals Second law
5I 6 · · Q , Btu/h 24,000 586 –494 –1380 –30,153 –207 0 –7648 · W , Btu/h 0 0 7635 0 0 0 0 7635 · ·· I , Btu/h·°R I I total , % 1.405 0.279 2.417 0.441 1.278 0 1.725 7.545 19 4 32 6 17 0 23 24,000 · m =  = 345 lb/h 106.4 – 36.8 Second law
7I1 · · Q · = m s1 – s7 – 7 1 TR 24,000 = 345 0.2291 – 0.0800 –  = 1.405 Btu/h 479.67 Suction Line: Energy balance · · Q 1 2 = m h 2 – h 1 = 345 108.1 – 106.4 = 586 Btu/h Second law · · 1Q 2 · 1I 2 = m s 2 – s 1 –  = 345 0.2330 – 0.2291 – 586 549.67 T0 = 0.279 Btu/h R Compressor: Energy balance · · · 2Q3 = m h 3 – h 2 + 2W3 = 345 128.8 – 108.1 – 3.0 2545 = – 494 Btu/h Second law · · 2Q3 · 2I 3 = m s 3 – s 2 – T0 = 345 0.2374 – 0.2330 – – 494 549.67 = 2.417 Btu/h Discharge Line: Energy balance
3Q 4 · · Q · = m s6 – s5 – 5 6 T0 = 345 0.0750 – 0.0761 – – 207 549.67 = 0 Btu/h R Expansion Device: Energy balance
67 · · Q = m h7 – h6 = 0 Second law
6I 7 · · = m s7 – s6 = 345 0.0800 – 0.0750 = 1.725 Btu/h R These results are summarized in Table 4. For the Carnot cycle, TR 479.67 COP Carnot =  =  = 6.852 T0 – TR 70 The Carnot power requirement for the 2 ton load is · Q evap 24 ,000 · =  =  = 3502 Btu/h W Carnot 6.852 COP Carnot The actual power requirement for the compressor is · · · W comp = W Carnot + I total T 0 = 3502 + 7.545 549.67 = 7649 Btu/h This result is within computational error of the measured power input to the compressor of 7635 Btu/h. R · · = m h4 – h3 = 345 124.8 – 128.8 = – 1380 Btu/h Second law
3I 4 · · Q · = m s4 – s3 – 3 4 T0 = 345 0.2314 – 0.2374 – – 1380 549.67 = 0.441 Btu/h R Condenser: Energy balance
4Q5 · · = m h5 – h4 = 345 37.4 – 124.8 = – 30,153 Btu/h Second law
4I 5 · · Q · = m s5 – s4 – 4 5 T0 = 345 0.0761 – 0.2314 – – 30,153 549.67 = 1.278 Btu/h R Liquid Line: Energy balance
56 · · Q = m h6 – h5 = 345 36.8 – 37.4 = – 207 Btu/h The analysis demonstrated in Example 5 can be applied to any actual vapor compression refrigeration system. The only required information for secondlaw analysis is the refrigerant thermodynamic state points and mass flow rates and the temperatures in which the system is exchanging heat. In this example, the extra compressor power required to overcome the irreversibility in each component is determined. The component with the largest loss is the compressor. This loss is due to motor inefficiency, friction losses, and irreversibilities caused by pressure drops, mixing, and heat transfer between the compressor and the surroundings. The unrestrained expansion in the expansion device is the next largest, but could be reduced by using an expander rather than a throttling process. An expander may be economical on large machines. All heat transfer irreversibilities on both the refrigerant side and the air side of the condenser and evaporator are included in the analysis. Refrigerant pressure drop is also included. Airside pressure drop irreversibilities of the two heat exchangers are not included, but these are equal to the fan power requirements because all the fan power is dissipated as heat. An overall secondlaw analysis, such as in Example 5, shows the designer components with the most losses, and helps determine which components should be replaced or redesigned to improve performance. However, it does not identify the nature of the losses; Thermodynamics and Refrigeration Cycles
Fig. 16 Thermal Cycles Qhot + Qcold = – Qmid (positive heat quantities are into the cycle) The second law requires that Q hot Q cold Q mid  +  + T hot T cold T mid 0 2.13
(44) (45) with equality holding in the ideal case. From these two laws alone (i.e., without invoking any further assumptions) it follows that, for the ideal forward cycle, T hot – T mid Q cold COP ideal =  = Q hot T hot T cold T mid – T cold (46) Fig. 16 Thermal Cycles this requires a more detailed secondlaw analysis of the actual processes in terms of fluid flow and heat transfer (Liang and Kuehn 1991). A detailed analysis shows that most irreversibilities associated with heat exchangers are due to heat transfer, whereas airside pressure drop causes a very small loss and refrigerant pressure drop causes a negligible loss. This finding indicates that promoting refrigerant heat transfer at the expense of increasing the pressure drop often improves performance. Using a thermoeconomic technique is required to determine the cost/benefits associated with reducing component irreversibilities. The heat ratio Qcold /Qhot is commonly called the coefficient of performance (COP), which is the cooling realized divided by the driving heat supplied. Heat rejected to ambient may be at two different temperatures, creating a fourtemperature cycle. The ideal COP of the fourtemperature cycle is also expressed by Equation (46), with Tmid signifying the entropic mean heat rejection temperature. In that case, Tmid is calculated as follows: Q mid hot + Q mid cold T mid = Q mid hot Q mid cold  + T mid hot T mid cold (47) ABSORPTION REFRIGERATION CYCLES
An absorption cycle is a heatactivated thermal cycle. It exchanges only thermal energy with its surroundings; no appreciable mechanical energy is exchanged. Furthermore, no appreciable conversion of heat to work or work to heat occurs in the cycle. Absorption cycles are used in applications where one or more of the exchanges of heat with the surroundings is the useful product (e.g., refrigeration, air conditioning, and heat pumping). The two great advantages of this type of cycle in comparison to other cycles with similar product are • No large, rotating mechanical equipment is required • Any source of heat can be used, including lowtemperature sources (e.g., waste heat) This expression results from assigning all the entropy flow to the single temperature Tmid. The ideal COP for the fourtemperature cycle requires additional assumptions, such as the relationship between the various heat quantities. Under the assumptions that Qcold = Qmid cold and Qhot = Qmid hot , the following expression results: T hot – T mid hot COP ideal = T hot T cold T mid cold T cold T mid hot (48) WORKING FLUID PHASE CHANGE CONSTRAINTS
Absorption cycles require at least two working substances: a sorbent and a fluid refrigerant; these substances undergo phase changes. Given this constraint, many combinations are not achievable. The first result of invoking the phase change constraints is that the various heat flows assume known identities. As illustrated in Figure 17, the refrigerant phase changes occur in an evaporator and a condenser, and the sorbent phase changes in an absorber and a desorber (generator). For the forward absorption cycle, the highesttemperature heat is always supplied to the generator, Qhot Qcold Qgen Qevap (49) IDEAL THERMAL CYCLE
All absorption cycles include at least three thermal energy exchanges with their surroundings (i.e., energy exchange at three different temperatures). The highest and lowesttemperature heat flows are in one direction, and the midtemperature one (or two) is in the opposite direction. In the forward cycle, the extreme (hottest and coldest) heat flows are into the cycle. This cycle is also called the heat amplifier, heat pump, conventional cycle, or Type I cycle. When the extremetemperature heat flows are out of the cycle, it is called a reverse cycle, heat transformer, temperature amplifier, temperature booster, or Type II cycle. Figure 16 illustrates both types of thermal cycles. This fundamental constraint of heat flow into or out of the cycle at three or more different temperatures establishes the first limitation on cycle performance. By the first law of thermodynamics (at steady state), and the coldest heat is supplied to the evaporator: (50) For the reverse absorption cycle, the highesttemperature heat is rejected from the absorber, and the lowesttemperature heat is rejected from the condenser. The second result of the phase change constraint is that, for all known refrigerants and sorbents over pressure ranges of interest, Qevap and Qgen Qcond Qabs (51) (52) These two relations are true because the latent heat of phase change (vapor condensed phase) is relatively constant when far removed from the critical point. Thus, each heat input cannot be independently adjusted. 2.14
The ideal singleeffect forwardcycle COP expression is COP ideal T gen – T abs T gen T evap T cond – T evap T cond T abs (53) 2009 ASHRAE Handbook—Fundamentals
Temperature Glide
One important limitation of simplified analysis of absorption cycle performance is that the heat quantities are assumed to be at fixed temperatures. In most actual applications, there is some temperature change (temperature glide) in the various fluids supplying or acquiring heat. It is most easily described by first considering situations wherein temperature glide is not present (i.e., truly isothermal heat exchanges). Examples are condensation or boiling of pure components (e.g., supplying heat by condensing steam). Any sensible heat exchange relies on temperature glide: for example, a circulating hightemperature liquid as a heat source; cooling water or air as a heat rejection medium; or circulating chilled glycol. Even latent heat exchanges can have temperature glide, as when a multicomponent mixture undergoes phase change. When the temperature glide of one fluid stream is small compared to the cycle lift or drop, that stream can be represented by an average temperature, and the preceding analysis remains representative. However, one advantage of absorption cycles is they can maximize benefit from lowtemperature, highglide heat sources. That ability derives from the fact that the desorption process inherently embodies temperature glide, and hence can be tailored to match the heat source glide. Similarly, absorption also embodies glide, which can be made to match the glide of the heat rejection medium. Implications of temperature glide have been analyzed for power cycles (Ibrahim and Klein 1998), but not yet for absorption cycles. Equality holds only if the heat quantities at each temperature may be adjusted to specific values, which is not possible, as shown the following discussion. The third result of invoking the phase change constraint is that only three of the four temperatures Tevap, Tcond , Tgen, and Tabs may be independently selected. Practical liquid absorbents for absorption cycles have a significant negative deviation from behavior predicted by Raoult’s law. This has the beneficial effect of reducing the required amount of absorbent recirculation, at the expense of reduced lift (Tcond – Tevap) and increased sorption duty. In practical terms, for most absorbents, Qabs /Qcond and Tgen – Tabs 1.2(Tcond – Tevap) (55) 1.2 to 1.3 (54) The net result of applying these approximations and constraints to the idealcycle COP for the singleeffect forward cycle is COP ideal T evap T cond 1.2 T gen T abs Q cond Q abs 0.8 (56) WORKING FLUIDS
Working fluids for absorption cycles fall into four categories, each requiring a different approach to cycle modeling and thermodynamic analysis. Liquid absorbents can be nonvolatile (i.e., vapor phase is always pure refrigerant, neglecting condensables) or volatile (i.e., vapor concentration varies, so cycle and component modeling must track both vapor and liquid concentration). Solid sorbents can be grouped by whether they are physisorbents (also known as adsorbents), for which, as for liquid absorbents, sorbent temperature depends on both pressure and refrigerant loading (bivariance); or chemisorbents, for which sorbent temperature does not vary with loading, at least over small ranges. Beyond these distinctions, various other characteristics are either necessary or desirable for suitable liquid absorbent/refrigerant pairs, as follows: Absence of Solid Phase (Solubility Field). The refrigerant/ absorbent pair should not solidify over the expected range of composition and temperature. If a solid forms, it will stop flow and shut down equipment. Controls must prevent operation beyond the acceptable solubility range. Relative Volatility. The refrigerant should be much more volatile than the absorbent so the two can be separated easily. Otherwise, cost and heat requirements may be excessive. Many absorbents are effectively nonvolatile. Affinity. The absorbent should have a strong affinity for the refrigerant under conditions in which absorption takes place. Affinity means a negative deviation from Raoult’s law and results in an activity coefficient of less than unity for the refrigerant. Strong affinity allows less absorbent to be circulated for the same refrigeration effect, reducing sensible heat losses, and allows a smaller liquid heat exchanger to transfer heat from the absorbent to the pressurized refrigerant/absorption solution. On the other hand, as affinity increases, extra heat is required in the generators to separate refrigerant from the absorbent, and the COP suffers. Pressure. Operating pressures, established by the refrigerant’s thermodynamic properties, should be moderate. High pressure requires heavywalled equipment, and significant electrical power may be needed to pump fluids from the lowpressure side to the highpressure side. Vacuum requires largevolume equipment and special means of reducing pressure drop in the refrigerant vapor paths. In practical terms, the temperature constraint reduces the ideal COP to about 0.9, and the heat quantity constraint further reduces it to about 0.8. Another useful result is Tgen min = Tcond + Tabs – Tevap (57) where Tgen min is the minimum generator temperature necessary to achieve a given evaporator temperature. Alternative approaches are available that lead to nearly the same upper limit on idealcycle COP. For example, one approach equates the exergy production from a “driving” portion of the cycle to the exergy consumption in a “cooling” portion of the cycle (Tozer and James 1997). This leads to the expression COP ideal T evap T cond  = T abs T gen (58) Another approach derives the idealized relationship between the two temperature differences that define the cycle: the cycle lift, defined previously, and drop (Tgen – Tabs). Fig. 17 SingleEffect Absorption Cycle Fig. 17 SingleEffect Absorption Cycle Thermodynamics and Refrigeration Cycles
Stability. High chemical stability is required because fluids are subjected to severe conditions over many years of service. Instability can cause undesirable formation of gases, solids, or corrosive substances. Purity of all components charged into the system is critical for high performance and corrosion prevention. Corrosion. Most absorption fluids corrode materials used in construction. Therefore, corrosion inhibitors are used. Safety. Precautions as dictated by code are followed when fluids are toxic, inflammable, or at high pressure. Codes vary according to country and region. Transport Properties. Viscosity, surface tension, thermal diffusivity, and mass diffusivity are important characteristics of the refrigerant/absorbent pair. For example, low viscosity promotes heat and mass transfer and reduces pumping power. Latent Heat. The refrigerant latent heat should be high, so the circulation rate of the refrigerant and absorbent can be minimized. Environmental Soundness. The two parameters of greatest concern are the global warming potential (GWP) and the ozone depletion potential (ODP). For more information on GWP and ODP, see Chapter 5 of the 2006 ASHRAE Handbook—Refrigeration. No refrigerant/absorbent pair meets all requirements, and many requirements work at crosspurposes. For example, a greater solubility field goes hand in hand with reduced relative volatility. Thus, selecting a working pair is inherently a compromise. Water/lithium bromide and ammonia/water offer the best compromises of thermodynamic performance and have no known detrimental environmental effect (zero ODP and zero GWP). Ammonia/water meets most requirements, but its volatility ratio is low and it requires high operating pressures. Ammonia is also a Safety Code Group B2 fluid (ASHRAE Standard 34), which restricts its use indoors. Advantages of water/lithium bromide include high (1) safety, (2) volatility ratio, (3) affinity, (4) stability, and (5) latent heat. However, this pair tends to form solids and operates at deep vacuum. Because the refrigerant turns to ice at 32°F, it cannot be used for lowtemperature refrigeration. Lithium bromide (LiBr) crystallizes at moderate concentrations, as would be encountered in aircooled chillers, which ordinarily limits the pair to applications where the absorber is watercooled and the concentrations are lower. However, using a combination of salts as the absorbent can reduce this crystallization tendency enough to allow air cooling (Macriss 1968). Other disadvantages include low operating pressures and high viscosity. This is particularly detrimental to the absorption step; however, alcohols with a high relative molecular mass enhance LiBr absorption. Proper equipment design and additives can overcome these disadvantages. Other refrigerant/absorbent pairs are listed in Table 5 (Macriss and Zawacki 1989). Several appear suitable for certain cycles and may solve some problems associated with traditional pairs. However, information on properties, stability, and corrosion is limited. Also, some of the fluids are somewhat hazardous. Table 5
Refrigerant H2O 2.15
Refrigerant/Absorbent Pairs
Absorbents Salts Alkali halides LiBr LiClO3 CaCl2 ZnCl2 ZnBr Alkali nitrates Alkali thiocyanates Bases Alkali hydroxides Acids H2SO4 H3PO4 H2O Alkali thiocyanates NMP E181 DMF Pyrrolidone Organic solvents NH3 TFE (Organic) SO2 • The Dühring diagram (solution temperature versus reference temperature) retains the linearity of the van’t Hoff plot but eliminates the complexity of nonlinear coordinates. Thus, it is used extensively (see Figure 20). The primary drawback is the need for a reference substance. • The Gibbs plot (solution temperature versus T ln P) retains most of the advantages of the Dühring plot (linear temperature coordinates, concentration contours are straight lines) but eliminates the need for a reference substance. • The Merkel plot (enthalpy versus concentration) is used to assist thermodynamic calculations and to solve the distillation problems that arise with volatile absorbents. It has also been used for basic cycle analysis. • Temperatureentropy coordinates are occasionally used to relate absorption cycles to their mechanical vapor compression counterparts. CONCEPTUALIZING THE CYCLE
The basic absorption cycle shown in Figure 17 must be altered in many cases to take advantage of the available energy. Examples include the following: (1) the driving heat is much hotter than the minimum required Tgen min: a multistage cycle boosts the COP; and (2) the driving heat temperature is below Tgen min: a different multistage cycle (halfeffect cycle) can reduce the Tgen min. Multistage cycles have one or more of the four basic exchangers (generator, absorber, condenser, evaporator) present at two or more places in the cycle at different pressures or concentrations. A multieffect cycle is a special case of multistaging, signifying the number of times the driving heat is used in the cycle. Thus, there are several types of twostage cycles: doubleeffect, halfeffect, and twostage, tripleeffect. Two or more singleeffect absorption cycles, such as shown in Figure 17, can be combined to form a multistage cycle by coupling any of the components. Coupling implies either (1) sharing component(s) between the cycles to form an integrated single hermetic cycle or (2) exchanging heat between components belonging to two hermetically separate cycles that operate at (nearly) the same temperature level. Figure 18 shows a doubleeffect absorption cycle formed by coupling the absorbers and evaporators of two singleeffect cycles ABSORPTION CYCLE REPRESENTATIONS
The quantities of interest to absorption cycle designers are temperature, concentration, pressure, and enthalpy. The most useful plots use linear scales and plot the key properties as straight lines. Some of the following plots are used: • Absorption plots embody the vaporliquid equilibrium of both the refrigerant and the sorbent. Plots on linear pressuretemperature coordinates have a logarithmic shape and hence are little used. • In the van’t Hoff plot (ln P versus –1/T ), the constant concentration contours plot as nearly straight lines. Thus, it is more readily constructed (e.g., from sparse data) in spite of the awkward coordinates. 2.16
Fig. 18 DoubleEffect Absorption Cycle Fig. 19 2009 ASHRAE Handbook—Fundamentals
Generic TripleEffect Cycles Fig. 18 DoubleEffect Absorption Cycle into an integrated, single hermetic cycle. Heat is transferred between the highpressure condenser and intermediatepressure generator. The heat of condensation of the refrigerant (generated in the hightemperature generator) generates additional refrigerant in the lowertemperature generator. Thus, the prime energy provided to the hightemperature generator is cascaded (used) twice in the cycle, making it a doubleeffect cycle. With the generation of additional refrigerant from a given heat input, the cycle COP increases. Commercial water/lithium bromide chillers normally use this cycle. The cycle COP can be further increased by coupling additional components and by increasing the number of cycles that are combined. This way, several different multieffect cycles can be combined by pressurestaging and/or concentrationstaging. The doubleeffect cycle, for example, is formed by pressurestaging two singleeffect cycles. Figure 19 shows twelve generic tripleeffect cycles identified by Alefeld and Radermacher (1994). Cycle 5 is a pressurestaged cycle, and Cycle 10 is a concentrationstaged cycle. All other cycles are pressure and concentrationstaged. Cycle 1, which is called a dualloop cycle, is the only cycle consisting of two loops that does not circulate absorbent in the lowtemperature portion of the cycle. Each of the cycles shown in Figure 19 can be made with one, two, or sometimes three separate hermetic loops. Dividing a cycle into separate hermetic loops allows the use of a different working fluid in each loop. Thus, a corrosive and/or highlift absorbent can be restricted to the loop where it is required, and a conventional additiveenhanced absorbent can be used in other loops to reduce system cost significantly. As many as 78 hermetic loop configurations can be synthesized from the twelve tripleeffect cycles shown in Figure 19. For each hermetic loop configuration, further variations are possible according to the absorbent flow pattern (e.g., series or parallel), the absorption working pairs selected, and various other hardware details. Thus, literally thousands of distinct variations of the tripleeffect cycle are possible. The ideal analysis can be extended to these multistage cycles (Alefeld and Radermacher 1994). A similar range of cycle variants is possible for situations calling for the halfeffect cycle, in which the available heat source temperature is below tgen min. Fig. 19 Generic TripleEffect Cycles Fig. 20 SingleEffect WaterLithium Bromide Absorption Cycle Dühring Plot Fig. 20 SingleEffect Water/Lithium Bromide Absorption Cycle Dühring Plot As an example of simulation, Figure 20 shows a Dühring plot of a singleeffect water/lithium bromide absorption chiller. The chiller is hotwaterdriven, rejects waste heat from the absorber and the condenser to a stream of cooling water, and produces chilled water. A simulation of this chiller starts by specifying the assumptions (Table 6) and the design parameters and operating conditions at the design point (Table 7). Design parameters are the specified UA values and the flow regime (co/counter/crosscurrent, pool, or film) of all heat exchangers (evaporator, condenser, generator, absorber, solution heat exchanger) and the flow rate of weak solution through the solution pump. One complete set of input operating parameters could be the design point values of the chilledwater and cooling water temper· atures tchill in, tchill out , tcool in, tcool out , hotwater flow rate m hot , and total cooling capacity Qe. With this information, a cycle simulation calculates the required hotwater temperatures; coolingwater flow rate; and temperatures, pressures, and concentrations at all internal state points. Some additional assumptions are made that reduce the number of unknown parameters. With these assumptions and the design parameters and operating conditions as specified in Table 7, the cycle simulation can be conducted by solving the following set of equations: ABSORPTION CYCLE MODELING Analysis and Performance Simulation
A physicalmathematical model of an absorption cycle consists of four types of thermodynamic equations: mass balances, energy balances, relations describing heat and mass transfer, and equations for thermophysical properties of the working fluids. Thermodynamics and Refrigeration Cycles
Table 6 Assumptions for SingleEffect Water/Lithium Bromide Model (Figure 20)
Assumptions • Generator and condenser as well as evaporator and absorber are under same pressure • Refrigerant vapor leaving the evaporator is saturated pure water • Liquid refrigerant leaving the condenser is saturated • Strong solution leaving the generator is boiling • Refrigerant vapor leaving the generator has the equilibrium temperature of the weak solution at generator pressure • Weak solution leaving the absorber is saturated • No liquid carryover from evaporator • Flow restrictors are adiabatic • Pump is isentropic • No jacket heat losses • The LMTD (log mean temperature difference) expression adequately estimates the latent changes Design Parameters Evaporator UAevap = 605,000 Btu/h·°F, countercurrent film Condenser Absorber Generator Solution General UAcond = 342,300 Btu/h·°F, countercurrent film UAabs = 354,300 Btu/h·°F, countercurrent filmabsorber UAgen = 271,800 Btu/h·°F, poolgenerator 2.17
Table 7 Design Parameters and Operating Conditions for SingleEffect Water/Lithium Bromide Absorption Chiller
Operating Conditions tchill in = 53.6°F tchill out = 42.8°F tcool out = 95°F tcool in = 80.6°F · m hot = 590,000 lb/h UAsol = 64,100 Btu/h·°F, countercurrent · · = 95,200 lb/h m Q
weak evap = 7.33 106 Btu/h Mass Balances · · · m refr + m strong = m weak · m strong Energy Balances · · Q evap = m h – h liq, cond refr vapor, evap · = m chill h chill in – h chill out · · Q cond = m h – h liq, cond refr vapor, gen · = m cool h cool out – h cool mean · · · Q abs = m refr h vapor, evap + m strong h strong, gen · · – m weak h weak, abs – Q sol · =m h –h
cool cool mean cool in s trong (59) (60) Table 8 Simulation Results for SingleEffect Water/Lithium Bromide Absorption Chiller
Internal Parameters Performance Parameters · Q evap = 7.33 106 Btu/h · m chill = 677,000 lb/h · Q cond = 7.92 106 Btu/h · m cool = 1.260 106 lb/h · Q abs = 10.18 106 Btu/h tcool,mean = 88.7°F · Q gen = 10.78 106 Btu/h thot in = 257°F thot out = 239°F · Q sol = 2.815 = 65.4% COP = 0.68 106 Btu/h · = m weak w eak Evaporator Condenser tvapor,evap = 35.2°F psat,evap = 0.1 psia Tliq,cond = 115.2°F psat,cond = 1.48 psia
weak = 59.6% tweak = 105.3°F tstrong,abs = 121.8°F (61) Absorber Generator (62) = 64.6% tstrong,gen = 218.3°F tweak,gen = 198.3°F tweak,sol = 169°F
strong Solution (63) General · · · Q gen = m refr h vapor, gen + m strong h strong, gen · · – m weak h – Q sol · = m hot h hot
weak, abs in tstrong,sol = 144.3°F tweak,sol = 169°F · m vapor = 7380 lb/h · m = 87,800 lb/h
strong – h hot out (64) · · Q sol = m strong h strong, gen – h strong, sol · =m h –h
weak weak, sol weak, abs t hot in – t strong, gen – t hot out – t weak, gen · Q gen = UA gen  (69) t hot in – t strong, gen ln t hot out – t weak, gen t strong, gen – t weak, sol – t strong, sol – t weak, abs · Q sol = UA sol t strong, gen – t weak, sol ln (70) t strong, sol – t weak, abs Fluid Property Equations at each state point Thermal Equations of State: TwoPhase Equilibrium: hwater (t, p), hsol (t, p, ) twater,sat ( p), tsol,sat ( p, ) (65) Heat Transfer Equations t chill in – t chill out · Q evap = UA evap t chill in – t vapor, evap ln t chill out – t vapor, evap t cool out – t cool mean · Q cond = UA cond t liq, cond – t cool mean ln t liq, cond – t cool out (66) (67) t strong, abs – t cool mean – t weak, abs – t cool in · Q abs = UA abs t strong, abs – t cool mean ln (68) t weak, abs – t cool in The results are listed in Table 8. A baseline correlation for the thermodynamic data of the H2O/ LiBr absorption working pair is presented in Hellman and Grossman (1996). Thermophysical property measurements at higher temperatures are reported by Feuerecker et al. (1993). Additional hightemperature measurements of vapor pressure and specific heat appear in Langeliers et al. (2003), including correlations of the data. DoubleEffect Cycle
Doubleeffect cycle calculations can be performed in a manner similar to that for the singleeffect cycle. Mass and energy balances 2.18
Fig. 21 DoubleEffect WaterLithium Bromide Absorption Cycle with State Points 2009 ASHRAE Handbook—Fundamentals
Table 9 Inputs and Assumptions for DoubleEffect WaterLithium Bromide Model (Figure 21)
Inputs Capacity Evaporator temperature Desorber solution exit temperature Condenser/absorber low temperature Solution heat exchanger effectiveness Assumptions • • • • • • • • • • • • • • Steady state Refrigerant is pure water No pressure changes except through flow restrictors and pump State points at 1, 4, 8, 11, 14, and 18 are saturated liquid State point 10 is saturated vapor Temperature difference between hightemperature condenser and lowtemperature generator is 9°F Parallel flow Both solution heat exchangers have same effectiveness Upper loop solution flow rate is selected such that upper condenser heat exactly matches lower generator heat requirement Flow restrictors are adiabatic Pumps are isentropic No jacket heat losses No liquid carryover from evaporator to absorber Vapor leaving both generators is at equilibrium temperature of entering solution stream · Q evap t10 t14 t1, t8 500 tons (refrig.) 41.1°F 339.3°F 108.3°F 0.6 Fig. 21 DoubleEffect Water/Lithium Bromide Absorption Cycle with State Points of the model shown in Figure 21 were calculated using the inputs and assumptions listed in Table 9. The results are shown in Table 10. The COP is quite sensitive to several inputs and assumptions. In particular, the effectiveness of the solution heat exchangers and the driving temperature difference between the hightemperature condenser and the lowtemperature generator influence the COP strongly. AMMONIA/WATER ABSORPTION CYCLES
Ammonia/water absorption cycles are similar to water/lithium bromide cycles, but with some important differences because of ammonia’s lower latent heat compared to water, the volatility of the absorbent, and the different pressure and solubility ranges. The latent heat of ammonia is only about half that of water, so, for the same duty, the refrigerant and absorbent mass circulation rates are roughly double that of water/lithium bromide. As a result, the sensible heat loss associated with heat exchanger approaches is greater. Accordingly, ammonia/water cycles incorporate more techniques to reclaim sensible heat, described in Hanna et al. (1995). The refrigerant heat exchanger (RHX), also known as refrigerant subcooler, which improves COP by about 8%, is the most important (Holldorff 1979). Next is the absorber heat exchanger (AHX), accompanied by a generator heat exchanger (GHX) (Phillips 1976). These either replace or supplement the traditional solution heat exchanger (SHX). These components would also benefit the water/lithium bromide cycle, except that the deep vacuum in that cycle makes them impractical there. The volatility of the water absorbent is also key. It makes the distinction between crosscurrent, cocurrent, and countercurrent mass exchange more important in all of the latent heat exchangers (Briggs 1971). It also requires a distillation column on the highpressure side. When improperly implemented, this column can impose both cost and COP penalties. Those penalties are avoided by refluxing the column from an internal diabatic section (e.g., solutioncooled rectifier [SCR]) rather than with an external reflux pump. The highpressure operating regime makes it impractical to achieve multieffect performance via pressurestaging. On the other hand, the exceptionally wide solubility field facilitates concentration staging. The generatorabsorber heat exchange (GAX) cycle is an especially advantageous embodiment of concentration staging (Modahl and Hayes 1988). Ammonia/water cycles can equal the performance of water/ lithium bromide cycles. The singleeffect or basic GAX cycle yields the same performance as a singleeffect water/lithium bromide
Point 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 Table 10 State Point Data for DoubleEffect Water/Lithium Bromide Cycle (Figure 21)
h, Btu/lb 50.6 50.6 78.3 106.2 76.1 76.1 1143.2 76.2 76.2 1078.6 86.7 86.7 129.4 162.7 116.4 116.4 1197.4 185.0 185.0 · m, lb/min 1263.4 1263.4 1263.4 1163.7 1163.7 1163.7 42.3 99.8 99.8 99.8 727.3 727.3 727.3 669.9 669.9 669.9 57.4 57.4 57.4 p, psia 0.13 1.21 1.21 1.21 1.21 0.13 1.21 1.21 0.13 0.13 1.21 16.21 16.21 16.21 16.21 1.21 16.21 16.21 1.21 Q, Fraction 0.0 t, °F 108.3 108.3 168.1 208.0 137.9 127.8 186.2 108.3 41.1 41.1 186.2 186.2 278.0 339.3 231.6 210.3 312.2 217.0 108.3 = 6.000 = 5.019 = 2.103 = 1.862 x, % LiBr 59.5 59.5 64.6 64.6 64.6 0.0 0.0 0.0 0.0 59.5 59.5 59.5 64.6 64.6 64.6 0.0 0.0 0.0 106 Btu/h 106 Btu/h 106 Btu/h 106 Btu/h 0.0 0.004 0.0 0.063 1.0 0.0 0.0 0.008 0.0 0.105 · Q evap · Q gen · Q shx 1 · Q shx 2 · Wp 1 · Wp 2 COP = 1.195 t = 9.0°F · Q abs · Q gen · Q cond = 0.600 = 7.936 = 3.488 = 3.085 106 106 Btu/h Btu/h = 0.032 hp = 0.258 hp 106 Btu/h cycle; the branched GAX cycle (Herold et al. 1991) yields the same performance as a water/lithium bromide doubleeffect cycle; and the VX GAX cycle (Erickson and Rane 1994) yields the same performance as a water/lithium bromide tripleeffect cycle. Additional Thermodynamics and Refrigeration Cycles
Table 11 Inputs and Assumptions for SingleEffect Ammonia/Water Cycle (Figure 22)
Inputs Capacity Highside pressure Lowside pressure Absorber exit temperature Generator exit temperature Rectifier vapor exit temperature Solution heat exchanger effectiveness Refrigerant heat exchanger effectiveness Assumptions • • • • • • • • • Steady state No pressure changes except through flow restrictors and pump States at points 1, 4, 8, 11, and 14 are saturated liquid States at point 12 and 13 are saturated vapor Flow restrictors are adiabatic Pump is isentropic No jacket heat losses No liquid carryover from evaporator to absorber Vapor leaving generator is at equilibrium temperature of entering solution stream · Q evap phigh plow t1 t4 t7
shx rhx 2.19
Table 12 State Point Data for SingleEffect Ammonia/Water Cycle (Figure 22)
h, Btu/lb –24.55 –24.05 38.47 83.81 10.61 10.61 579.51 76.61 35.28 35.28 522.55 563.88 613.91 51.72 · m, lb/min 1408.2 1408.2 1408.2 1203.0 1203.0 1203.0 205.2 205.2 205.2 205.2 205.2 205.2 209.9 4.6 p, psia 74.7 211.8 211.8 211.8 211.8 74.7 211.8 211.8 211.8 74.7 74.7 74.7 211.8 211.8 Q, Fraction 0.0 t, °F 105.0 105.5 163.0 203.0 135.6 132.0 131.0 100.1 64.1 41.1 42.8 87.0 174.5 174.5 = 6.00 = 1.051 = 5.089 = 5.805 = 5.283 = 9.22 hp x, Fraction NH3 0.50094 0.50094 0.50094 0.41612 0.41612 0.41612 0.99809 0.99809 0.99809 0.99809 0.99809 0.99809 0.98708 0.50094 500 tons (refrig.) 211.8 psia 74.7 psia 105°F 203°F 131°F 0.692 0.629 Point 1 2 3 4 5 6 7 8 9 10 11 12 13 14 0.0 0.006 1.0 0.0 0.049 0.953 1.0 1.0 0.0 · Q evap · Q gen · Q rhx · Qr · Q shx · W COP = 0.571 trhx = 36.00°F tshx = 30.1°F
rhx 106 Btu/h 107 Btu/h 105 Btu/h 105 Btu/h 106 Btu/h Fig. 22 SingleEffect AmmoniaWater Absorption Cycle = 0.629 = 0.692 = 9.784 = 6.192 106 Btu/h 106 Btu/h · Q abs · Q cond shx Fig. 22 SingleEffect Ammonia/Water Absorption Cycle advantages of the ammonia/water cycle include refrigeration capability, aircooling capability, all mild steel construction, extreme compactness, and capability of direct integration into industrial processes. Between heatactivated refrigerators, gasfired residential air conditioners, and large industrial refrigeration plants, this technology has accounted for the vast majority of absorption activity over the past century. Figure 22 shows the diagram of a typical singleeffect ammoniawater absorption cycle. The inputs and assumptions in Table 11 are used to calculate a singlecycle solution, which is summarized in Table 12. Comprehensive correlations of the thermodynamic properties of the ammonia/water absorption working pair are found in Ibrahim and Klein (1993) and TillnerRoth and Friend (1998a, 1998b), both of which are available as commercial software. Figure 29 in Chapter 30 of this volume was prepared using the Ibrahim and Klein correlation, which is also incorporated in REFPROP7 (National Institute of Standards and Technology). Transport properties for ammonia/water mixtures are available in IIR (1994) and in Melinder (1998). · I = irreversibility rate, Btu/h·°R m = mass, lb · m = mass flow, lb/min p = pressure, psia Q = heat energy, Btu · Q = rate of heat flow, Btu/h R = ideal gas constant, ft·lb/lb·°R s = specific entropy, Btu/lb·°R S = total entropy, Btu/°R t = temperature, °F T = absolute temperature, °R u = internal energy, Btu/lb v = specific volume, ft3/lb V = velocity of fluid, ft/s W = mechanical or shaft work, Btu · W = rate of work, power, Btu/h x = mass fraction (of either lithium bromide or ammonia) x = vapor quality (fraction) z = elevation above horizontal reference plane, ft Z = compressibility factor = heat exchanger effectiveness = efficiency = density, lb/ft3 Subscripts abs = absorber cg = condenser to generator cond = condenser or cooling mode evap = evaporator fg = fluid to vapor gen = generator gh = hightemperature generator o, 0 = reference conditions, usually ambient p = pump R = refrigerating or evaporator conditions rhx = refrigerant heat exchanger shx = solution heat exchanger sol = solution SYMBOLS
cp COP g h I = = = = = specific heat at constant pressure, Btu/lb·°F coefficient of performance local acceleration of gravity, ft/s2 enthalpy, Btu/lb irreversibility, Btu/°R 2.20
REFERENCES
Alefeld, G. and R. Radermacher. 1994. Heat conversion systems. CRC Press, Boca Raton. Benedict, M. 1937. Pressure, volume, temperature properties of nitrogen at high density, I and II. Journal of American Chemists Society 59(11): 22242233 and 22332242. Benedict, M., G.B. Webb, and L.C. Rubin. 1940. An empirical equation for thermodynamic properties of light hydrocarbons and their mixtures. Journal of Chemistry and Physics 4:334. Briggs, S.W. 1971. Concurrent, crosscurrent, and countercurrent absorption in ammoniawater absorption refrigeration. ASHRAE Transactions 77(1):171. Cooper, H.W. and J.C. Goldfrank. 1967. BWR constants and new correlations. Hydrocarbon Processing 46(12):141. Erickson, D.C. and M. Rane. 1994. Advanced absorption cycle: Vapor exchange GAX. Proceedings of the International Absorption Heat Pump Conference, Chicago. Feuerecker, G., J. Scharfe, I. Greiter, C. Frank, and G. Alefeld. 1993. Measurement of thermophysical properties of aqueous LiBr solutions at high temperatures and concentrations. Proceedings of the International Absorption Heat Pump Conference, New Orleans, AES30, pp. 493499. American Society of Mechanical Engineers, New York. Hanna, W.T., et al. 1995. Pinchpoint analysis: An aid to understanding the GAX absorption cycle. ASHRAE Technical Data Bulletin 11(2). Hellman, H.M. and G. Grossman. 1996. Improved property data correlations of absorption fluids for computer simulation of heat pump cycles. ASHRAE Transactions 102(1):980997. Herold, K.E., et al. 1991. The branched GAX absorption heat pump cycle. Proceedings of Absorption Heat Pump Conference, Tokyo. Hirschfelder, J.O., et al. 1958. Generalized equation of state for gases and liquids. Industrial and Engineering Chemistry 50:375. Holldorff, G. 1979. Revisions up absorption refrigeration efficiency. Hydrocarbon Processing 58(7):149. Howell, J.R. and R.O. Buckius. 1992. Fundamentals of engineering thermodynamics, 2nd ed. McGrawHill, New York. Hust, J.G. and R.D. McCarty. 1967. Curvefitting techniques and applications to thermodynamics. Cryogenics 8:200. Hust, J.G. and R.B. Stewart. 1966. Thermodynamic property computations for system analysis. ASHRAE Journal 2:64. Ibrahim, O.M. and S.A. Klein. 1993. Thermodynamic properties of ammoniawater mixtures. ASHRAE Transactions 99(1):14951502. Ibrahim, O.M. and S.A. Klein. 1998. The maximum power cycle: A model for new cycles and new working fluids. Proceedings of the ASME Advanced Energy Systems Division, AES vol. 117. American Society of Mechanical Engineers. New York. IIR. 1994. R123—Thermodynamic and physical properties. NH3–H2O. International Institute of Refrigeration, Paris. Kuehn, T.H. and R.E. Gronseth. 1986. The effect of a nonazeotropic binary refrigerant mixture on the performance of a single stage refrigeration cycle. Proceedings of the International Institute of Refrigeration Conference, Purdue University, p. 119. Langeliers, J., P. Sarkisian, and U. Rockenfeller. 2003. Vapor pressure and specific heat of LiBr H2O at high temperature. ASHRAE Transactions 109(1):423427. Liang, H. and T.H. Kuehn. 1991. Irreversibility analysis of a water to water mechanical compression heat pump. Energy 16(6):883. Macriss, R.A. 1968. Physical properties of modified LiBr solutions. AGA Symposium on Absorption AirConditioning Systems, February. Macriss, R.A. and T.S. Zawacki. 1989. Absorption fluid data survey: 1989 update. Oak Ridge National Laboratories Report ORNL/Sub8447989/4. Martin, J.J. and Y. Hou. 1955. Development of an equation of state for gases. AIChE Journal 1:142. 2009 ASHRAE Handbook—Fundamentals
Martz, W.L., C.M. Burton, and A.M. Jacobi. 1996a. Liquidvapor equilibria for R22, R134a, R125, and R32/125 with a polyol ester lubricant: Measurements and departure from ideality. ASHRAE Transactions 102(1):367374. Martz, W.L., C.M. Burton, and A.M. Jacobi. 1996b. Local composition modeling of the thermodynamic properties of refrigerant and oil mixtures. International Journal of Refrigeration 19(1):2533. Melinder, A. 1998. Thermophysical properties of liquid secondary refrigerants. Engineering Licentiate Thesis, Department of Energy Technology, The Royal Institute of Technology, Stockholm. Modahl, R.J. and F.C. Hayes. 1988. Evaluation of commercial advanced absorption heat pump. Proceedings of the 2nd DOE/ORNL Heat Pump Conference, Washington, D.C. NASA. 1971. Computer program for calculation of complex chemical equilibrium composition, rocket performance, incident and reflected shocks and ChapmanJouguet detonations. SP273. U.S. Government Printing Office, Washington, D.C. Phillips, B. 1976. Absorption cycles for aircooled solar air conditioning. ASHRAE Transactions 82(1):966. Dallas. Stewart, R.B., R.T. Jacobsen, and S.G. Penoncello. 1986. ASHRAE thermodynamic properties of refrigerants. Strobridge, T.R. 1962. The thermodynamic properties of nitrogen from 64 to 300 K, between 0.1 and 200 atmospheres. National Bureau of Standards Technical Note 129. Stoecker, W.F. and J.W. Jones. 1982. Refrigeration and air conditioning, 2nd ed. McGrawHill, New York. Tassios, D.P. 1993. Applied chemical engineering thermodynamics. SpringerVerlag, New York. Thome, J.R. 1995. Comprehensive thermodynamic approach to modeling refrigerantlubricant oil mixtures. International Journal of Heating, Ventilating, Air Conditioning and Refrigeration Research 1(2): 110. TillnerRoth, R. and D.G. Friend. 1998a. Survey and assessment of available measurements on thermodynamic properties of the mixture {water + ammonia}. Journal of Physical and Chemical Reference Data 27(1)S: 4561. TillnerRoth, R. and D.G. Friend. 1998b. A Helmholtz free energy formulation of the thermodynamic properties of the mixture {water + ammonia}. Journal of Physical and Chemical Reference Data 27(1)S:6396. Tozer, R.M. and R.W. James. 1997. Fundamental thermodynamics of ideal absorption cycles. International Journal of Refrigeration 20 (2):123135. BIBLIOGRAPHY
Bogart, M. 1981. Ammonia absorption refrigeration in industrial processes. Gulf Publishing Co., Houston. Herold, K.E., R. Radermacher, and S.A. Klein. 1996. Absorption chillers and heat pumps. CRC Press, Boca Raton. Jain, P.C. and G.K. Gable. 1971. Equilibrium property data for aquaammonia mixture. ASHRAE Transactions 77(1):149. Moran, M.J. and H. Shapiro. 1995. Fundamentals of engineering thermodynamics, 3rd ed. John Wiley & Sons, New York. Pátek, J. and J. Klomfar. 1995. Simple functions for fast calculations of selected thermodynamic properties of the ammoniawater system. International Journal of Refrigeration 18(4):228234. Stoecker, W.F. 1989. Design of thermal systems, 3rd ed. McGrawHill, New York. Van Wylen, C.J. and R.E. Sonntag. 1985. Fundamentals of classical thermodynamics, 3rd ed. John Wiley & Sons, New York. Zawacki, T.S. 1999. Effect of ammoniawater mixture database on cycle calculations. Proceedings of the International Sorption Heat Pump Conference, Munich. ...
View
Full
Document
This note was uploaded on 03/08/2011 for the course ASME 293 taught by Professor Range during the Spring '11 term at Prairie View A & M.
 Spring '11
 range

Click to edit the document details