In this chapter, the heat transfer between supercritical fluid flows and solid walls and that between compressible flows and solid walls is described. First, the physical fundamentals of supercritical fluids and compressible flows are explained. Second, methods for estimating the heat‐transfer performance according to the physical fundamentals and conventional experimental results are described. Then, the known correlations for estimating the heat‐transfer performance are introduced. Finally, examples of practical heat exchangers using supercritical fluid flows and/or compressible flows are presented.
- supercritical fluid flow
- compressible flow
- nusselt number
- reynolds number
- mach number
- pressure coefficient distribution
The range of use of heat exchangers is being expanded to extensive applications in various fields. In particular, supercritical fluids and high‐speed air, that is,, compressible fluids, are suitable as working fluids.
Supercritical fluid is a phase of substances, in addition to the solid, liquid, and gas phases. In particular, in the vicinity of the critical point, many physical properties behave in an unusual way. For example, the density, viscosity, and thermal conductivity drastically change at the critical point, the specific heat and thermal expansion ratios diverge at the critical point, and the sound velocity is zero at the critical point. The physical properties of a supercritical fluid must be evaluated by the appropriate equation of state and equation of the transport properties.
On the other hand, a compressible flow can be assumed as an ideal gas, but additional dynamic energy, that is, the Mach‐number effect, must be considered. Therefore, three types of pressures (static, total, and dynamic), four types of temperatures (static, total, dynamic, and recovery), the difference between laminar and turbulent boundary layers, etc., should be distinguished and treated.
2. Equations of state and transport properties of supercritical fluid
Figure 1 shows the
The vaporization curve ends at the critical point. On the vaporization curve, liquid is called the saturation liquid, and gas is called the saturation gas (vapor). When approaching the critical point along the vaporization curve, the density of the saturation liquid decreases, and the density of the saturation gas (vapor) increases. Finally, they meet at the critical point. Fluid overtaking the critical point in temperature and pressure is called the “supercritical fluid.”
The phase is thermodynamically determined by the Gibbs free energy :
Where is the enthalpy, is the entropy, is the internal energy, and is the specific volume .
That is, the phase is determined by the balance between the diffusivity caused by the thermal mobility of the molecules and the condensability by intermolecular forces. The diffusivity caused by thermal mobility increases with the temperature. The condensability by intermolecular forces increases with the density. In general, the following relationships hold:
|Solid||Diffusivity << condensability|
|Liquid||Diffusivity < condensability|
|Supercritical fluid||Diffusivity ≈ condensability|
|Gas (vapor)||Diffusivity > condensability|
|Gas (ideal gas)||Diffusivity >> condensability|
In Figure 1, the first‐order differentials of the Gibbs free energy
are discontinuous across the three coexistence curves, but the first‐order differentials of the Gibbs free energy are continuous at the critical point. In addition, the second‐order differentials of the Gibbs free energy are discontinuous at the critical point.
Here, is the density, is the isobaric specific heat, and is the isothermal compressibility. At the critical point, the density drastically changes, the specific heat and thermal expansion ratio diverge, and the sound velocity is zero.
Figures 2 and 3 show the isobaric and isothermal changes of the density, viscosity, and kinematic viscosity by using the data from references [2, 3]. Both the density (derived from the equation of state) and the viscosity (derived from the equation of the transport properties) drastically change at the critical point, and the derivatives with respect to temperature and pressure diverge at the critical point. The kinematic viscosity (combined with the density and viscosity) has an extremum value at the critical point. The equations of state and the transport properties should consider these types of tricky features in the vicinity of the critical point for transcritical‐ and supercritical‐fluid flows.
The most important substances in practical applications are carbon dioxide and water, although all substances have a supercritical‐fluid phase. Recently, accurate correlations for the equations of state and the transport properties containing the critical point have been proposed.
For carbon dioxide, Span and Wagner proposed the equation of state from the triple point to 1100 K at pressures up to 800 MPa . Their equation of state is briefly introduced here. They expressed the fundamental equation in the form of the Helmholtz energy
with two independent variables—the density and temperature . The dimensionless Helmholtz energy is divided into a part obeying the ideal gas behavior and a part that deviates from the ideal gas behavior :
Where is the reduced density; is the inverse reduced temperature; and and are the density and temperature, respectively, at the critical point. Then, all of the other thermodynamic properties can be obtained by the combined derivatives of Eq. (7) using the Maxwell relations .
Isochoric specific heat
Isobaric specific heat
Saturated specific heat
Speed of sound
For carbon dioxide, Vesovic et al. proposed transport properties in the temperature range of 200–1500 K for the viscosity and in the temperature range of 200–1000 K for the thermal conductivity . Their equations of the transport properties and are briefly introduced. Their fundamental equation combines three independent parts: a part obeying the ideal gas behavior and , a part with excess properties because of the elevated density and , and a part with an enhancement in the vicinity of the critical point and :
For water, Wagner and Pruß proposed the equation of state for the temperature range of 251.2–1273 K and pressures up to 1000 MPa . Huber et al. proposed the transport properties from the melting temperature to 1173 K at 1000 MPa [5, 6].
3. Heat transfers between supercritical fluid flow and solid
As mentioned in Section 2, the kinematic viscosity of a supercritical fluid is less than those of a liquid and gas; therefore, the Reynolds number, Re, of a supercritical fluid flow is higher than those of a liquid and gas flow with the same velocity, and a turbulent flow is easily formed. For heat transfer in a turbulent flow, Dittus and Boelter proposed a correlation of the Nusselt number using the and Prandtl number, , for a liquid flow in a circular automobile radiator  as shown in Figure 4.
Here, the superscript for or for , is the average velocity across the cross section, is the diameter of the tube, is the viscosity, is the mass flow rate, is the thermal diffusivity, and is the heat conductivity. For liquid and gas flows, the fluid properties and flow conditions can be regarded as constant throughout the entire region in most practical cases because the fluid properties are insensitive to temperature and pressure changes in the tube. Therefore, the inlet values of the physical properties and flow conditions can be used, and and can be regarded as constant throughout the entire tube. On the other hand, the fluid properties of a supercritical fluid are very sensitive to temperature and pressure changes in the tube. Thus, in the tube, the density gradually changes because of the heat input and/or pressure loss, the local average velocity changes, and even and change. Unfortunately, the Dittus‐Boelter correlation with the inlet values of the physical properties and flow conditions cannot be directly used for heat transfer in a supercritical turbulent flow. Liao and Zhao measured the rate of the heat transfer between a supercritical carbon dioxide flow and a circular solid tube wall for . Their tube was set in the horizontal direction. They proposed a correlation of area‐averaged Nusselt numbers as functions of the Reynolds and Prandtl numbers defined at the temperatures of the mean bulk and the wall.
Here, and are constant. This correlation is applicable in the range of 7.4 MPa < < 12.0 MPa, 20°C < < 110°C, 2°C < < 30°C, 0.02 kg/min < < 0.2 kg/min, 1025 < < 1022 for the horizontal long tubes of 0.50 mm < < 2.16 mm. and were originally derived from the Dittus‐Boelter correlation. is the effect of buoyancy in the radial direction of a horizontal tube. The density of fluid at a temperature and pressure in the vicinity of the critical point is very sensitive to changes in temperature; thus, the effect of the buoyancy derived from the temperature difference between the bulk and wall cannot be ignored. This effect is enhanced as the diameter of the tube increases.
Ito et al. proposed an airfoil heat exchanger, which is applied between a compressible airflow and a liquid or a supercritical fluid flow . It has an outer airfoil shape suitable for high‐speed airflow and contains several tubes for a high‐pressure liquid or a supercritical fluid flow. The researchers installed a cascade of airfoil heat exchangers into a subsonic wind tunnel at a temperature of and measured the heat‐transfer coefficient of a liquid or a supercritical fluid flow at a temperature of in a vertical tube. They derived correlations for supercritical carbon dioxide and compressed water at a pressure of MPa as follows:
These correlations are very simple and similar to the Dittus‐Boelter correlation in Eq. (20) but have sufficient accuracy. Ito et al. used accurate equations of state and the transport properties, as mentioned in Section 2. They said in reference  that ordinary correlations (of course, containing the Dittus‐Boelter correlation) for liquid and gas can be used when sufficiently accurate equations of state and the transport properties are used. However, the physical properties at a temperature and pressure in the vicinity of the critical point continuously change throughout the tube because of the heat input and/or pressure loss; therefore, changes in these physical properties throughout the tube should be sufficiently considered. For example, the present author recommends the numerical integration of local heat transfer correlations using local accurate physical properties for the entire tube.
4. Thermofluid dynamics of compressible flow on solid wall
4.1. Meanings of temperature and pressure of compressible flow
A stationary fluid pressure of [Pa], specific volume of [m3/kg], and constant temperature stores a mechanical energy of [J/kg]. Here,
The “pressure” (often called “static pressure”) is the potential of the mechanical energy level contained in a stationary fluid. A motional fluid has an additional dynamic energy [J/kg]:
in addition to ; therefore,
Here, [Pa] is called “dynamic pressure” and is an index of the dynamic mechanical energy level contained in a motional fluid. Further, [J/kg] is called “total mechanical energy.” Moreover, [Pa] is called the “total pressure” and is an index of the total mechanical energy level contained in a motional fluid. Some processes are reversible between mechanical energies of and in cases where and transform in the equilibrium processes. For example, using a nozzle, increases,
Next, we consider thermal energy. A stationary fluid at an isochoric specific heat of [J/(kg K)] stores a relative internal energy of [J/kg] from at the standard temperature :
Here, the internal energy is an index of the thermal energy level contained in a stationary fluid. In the case of a constant ,
The “temperature” (often called “static temperature”) is an index of the energy level contained in a stationary fluid.
In cases where a fluid is assumed as an ideal gas,
where is the gas constant, and is the density, which is equal to . Then,
A stationary fluid at an isochoric specific heat of [J/(kg K)] stores a relative enthalpy of [J/kg] from at the standard temperature of , a pressure of , and a specific volume of . Videlicet, enthalpy is a combination of internal energy and mechanical energy. Here,
In the case of a constant ,
where is the isobaric specific heat. A motional fluid has an additional dynamic energy [J/kg], as shown in Eq. (35). If a motional fluid suddenly stops, dynamic energy can be converted into enthalpy. Then, the following equation applies:
Here, [K] is called the “dynamic temperature” and is an index of the dynamic energy level contained in a motional fluid. Moreover, [K] is called the “total temperature” and is an index of the total energy level contained in a motional fluid. Some processes are reversible between mechanical energies of and in cases where transforms into in equilibrium processes. For example, using a nozzle, in an acceleration section, increases,
4.2. Isentropic change and sound speed of ideal gas
The specific heat ratio is defined as:
The change in the entropy is defined as:
When isentropic change ,
We totally differentiate Eq. (41), obtaining the following:
The sound speed is defined as:
4.3. Relationships of static and total values in isentropic compressible flow
The one‐dimensional energy equation of an isentropic flow at an arbitrary cross section is derived by using Eq. (46) as:
When the enthalpy and velocity are and at an arbitrary cross section 1,
This relationship is true even if cross section 1 corresponds to the stagnant cross section 0 ( and ); therefore,
We multiply by and substitute Eq. (66), obtaining the following:
At the stagnant cross section 0, the static temperature is equal to the total temperature ; therefore,
4.4. Relationships of local Mach number, pressure and temperature of flows on adiabatic walls
Figure 5 shows the pressure distribution on a plane and an airfoil. On both the plane and the airfoil, boundary layers are formed. The pressure in a boundary layer is almost equal to the pressure in a main flow outside of the boundary layer; therefore, the pressure in a boundary layer can be expressed by using relationships of the isentropic main flow. That is, . Afterwards, both the pressures are expressed as .
The pressure distribution on a solid wall is usually expressed by pressure coefficient , which is defined as:
but is sometimes expressed by another pressure coefficient , which is defined as:
The two expressions are related as follows:
On a plane, is unity everywhere; thus, is constant everywhere. On the other hand, on an airfoil, varies with the location; thus, varies.
Figure 6 shows the temperature distribution on an adiabatic plane and an airfoil. In flows on an adiabatic wall, the total temperature remains constant at the inlet total temperature . For incompressible flows, that is, with the Mach number , the static temperature is always the same as . Then, remains constant everywhere on both an adiabatic plane and an airfoil. On the other hand, for compressible flows, the Mach number varies according to the following equation, which is derived from Eq. (74):
Here, the static temperature varies with respect to for compressible flows.
On an adiabatic plane, is constant. Thus, remains constant anywhere on an adiabatic plane, even in cases of compressible flows. On the other hand, on an adiabatic airfoil, varies with the location; therefore, varies in cases of compressible flows.
4.5. Recovery temperature definition in boundary layer in compressible flow on adiabatic, heating and cooling walls
Eckert surveyed and organized the heat transfer in a boundary layer in a compressible flow on a wall . In a boundary layer on an adiabatic plane, the adiabatic‐wall temperature reaches . This is called the “recovery temperature.” Figure 7 shows a schematic of the total temperature and static temperature profiles, as well as the recovery temperature in the vicinity of an adiabatic solid surface with a boundary layer in a compressible flow. As described in Section 4.1, a compressible flow has a measurable dynamic energy; then, the static temperature in a boundary layer increases because of the braking effect, which converts a dynamic energy to a thermal energy. At the same time, heat generated by the braking effect conducts to the outside of the boundary layer. Therefore, the static temperature and total temperature in the boundary layer approach the recovery temperature on the wall, as shown in the middle in Figure 7.
In cases where a thermal boundary layer is completely inside a momentum boundary layer, that is, Pr ≥ 1 the heat generated by the braking effect uses the rise of the static temperature . The recovery temperature on an adiabatic wall is equal to the total temperature of the main flow outside of the boundary layer. On the other hand, in cases where a thermal boundary layer protrudes from the edge of a momentum boundary layer, that is, , only part of the heat generated by the braking effect uses the rise of the static temperature ; then, the recovery temperature on an adiabatic wall has an intermediate value between the total temperature and the static temperature of the main flow outside of the boundary layer. Eckert proposed an equation for the local recovery temperature on an adiabatic wall.
Here, is the “temperature recovery factor,” which is the ratio of the recovery temperature to the dynamic temperature of the main flow. Eckert mentioned that heat flux in a boundary layer in a compressible flow should be defined as:
where is the local heat transfer coefficient between a compressible flow and a solid wall. In the case where , the local wall temperature equals the recovery temperature and is called the “adiabatic wall temperature.”
Here, Eckert's theory is extended to the recovery temperature on a heating and cooling wall. In Eq. (80), the first term expressed by the static temperature represents the internal energy that a local boundary layer originally has, and the second term expressed by the dynamic temperature represents the net dynamic energy that is used to increase the temperature in a local boundary layer. When a local boundary layer is heated or cooled, the first term is affected, but the second term remains constant. The first term should be replaced by the appropriate form suitable for the heating or cooling of a boundary layer. Heating or cooling affects only a thermal boundary layer; therefore, the local total temperature at the location in the flow direction is defined as follows:
where and are the static temperature and density, respectively, in a heated or cooled boundary layer, and and are thermal boundary layer thickness and average velocity, respectively. Here, evaluations of and are used for a plane, but more appropriate expression for a particular target flow field can be used. Finally, Eq. (80) is replaced by the following equation for the local recovery temperature of a heated or cooled boundary layer.
5. Mach‐number distribution on solid walls with various shapes
As described in Section 4 4, the local Mach number is constant on a plane but varies with the location on a single airfoil or an airfoil in a cascade. For a single airfoil, when the inlet Mach number , the Reynolds number with a representative length of the airfoil chord , and the angle of attack are fixed, as
the distribution of the local pressure coefficient or is uniquely obtained. In cases of a cascade of airfoils, when the stagger angle and the solidity are fixed (see Figure 8), the distribution of the local pressure coefficient or is obtained. Fortunately, many experimental results of or have been reported for single airfoils and cascades of airfoils. The distributions of are calculated using Eqs. (75), (76), and (78).
6. Air‐temperature distribution in boundary layers on solid walls
Nishiyama described in his book  that a developing boundary layer transforms from a laminar boundary layer to a turbulent boundary layer at in regions with adverse pressure gradients, but a developing boundary layer transforms at in regions with favorable pressure gradients. This means that a developing boundary layer transforms across the minimum pressure point, that is, the maximum of the pressure coefficient or on the airfoil surface in cases of . According to the left graph of Figure 9, a developing boundary layer may transform at on the lower concave surface and at on the upper convex surface. Then, the local recovery temperature is assumed by using Eqs. (81) and (88) (see Figure 10). This can be used for the evaluation of the local heat flux using Eq. (82) if an adequate heat‐transfer coefficient is employed.
7. Heat transfer through practical heat exchanger with complex shape
Ito et al. evaluated the rate of heat transfer from a hot compressible airflow to a cold supercritical‐fluid flow through an airfoil heat exchanger, as shown in Figure 8 . Heat is transferred from the hot compressible airflow to the outer surface of the airfoil heat exchanger and is conducted from the outer surface to the five inner surfaces in the airfoil heat exchanger. Then, heat is transferred from the five inner surfaces of the airfoil heat exchanger to the cold supercritical‐fluid flow inside the five tubes.
First, Ito et al. conducted wind‐tunnel experiments. They installed thermocouples into the airfoil heat exchanger and experimentally measured the temperature at points inside the exchanger. Simultaneously, the air temperature and the air Mach number at the inlet, the supercritical‐fluid temperature and pressure at the inlet, and the supercritical‐fluid temperature at the outlet were experimentally measured.
Second, they assumed heat‐transfer coefficients to for the
Third, they performed an inverse heat‐conduction analysis. The boundary conditions were set according to the experimental results for the distribution of the recovery temperature using the methods described in Sections 4.6, as well as the inlet supercritical‐fluid temperature and pressure. Using these boundary conditions, heat‐conduction calculations for the airfoil heat exchanger were conducted, and the temperatures at the
Finally, the numerically obtained temperatures were compared with experimentally obtained temperatures. If the temperatures were equal, the assumed to and were true. Otherwise, the assumed to and were corrected, and the inverse heat‐conduction analysis was repeated.
They also obtained a supercritical‐fluid Nusselt number correlation for the tube flow given by Eq. (33).
Moreover, the heat‐transfer rate of an airfoil heat exchanger is estimated as follows:
where is a correction factor for the airfoil heat exchanger, and is the ratio of the actual heat‐transfer rate to the heat‐transfer rate of the ideal counter‐flow heat exchanger without thermal resistance.
Here, is an incidence of air at the inlet. The incidence is a flow‐direction angle from the airfoil camber (center) line at its leading edge, corresponding to an angle of attack of for the cascade in Figure 8. and indicate the temperature effectiveness, as follows:
Here, and are positive for an air‐cooled system and negative for an air‐heated system. is the ratio of the heat‐capacity rates.
Here, and are the mass flow rates of a supercritical‐fluid and air, respectively, for an airfoil heat exchanger, and and are the specific heats of a supercritical‐fluid and air, respectively. is the overall heat‐transfer coefficient for an ideal counter‐flow heat exchanger without thermal resistance.
Here, and are areas of supercritical‐fluid‐contact and air‐contact surfaces, respectively, for an airfoil heat exchanger. is the logarithmic mean temperature difference:
Φ is the ratio of the logarithmic mean temperature difference to the temperature difference between the inlet air temperature and the supercritical‐fluid temperature.
The actual heat‐exchange rate is estimated as .
For example, Ito et al. performed cycle calculations for an intercooled and recuperated jet engine employing several pairs of airfoil heat exchangers whose heat‐transfer performance is evaluated by Eqs. (91)–(99) .
These examples can be used for a cascade of airfoil heat exchangers; therefore, the air Nusselt number correlation in Eq. (91) or thermal resistance in Eq. (93) might be further modified in the near future according to the progress of research, as knowledge in this field is still developing.
The Nusselt number between supercritical fluid flows and solid walls can be estimated by appropriate conventional correlations using the Reynolds and Prandtl numbers if sufficiently accurate physical properties are used for each local point through the region of supercritical fluid flows. Thus, a numerical integration of local heat flow rate is required when you calculate the entire heat flow rate in a heat exchanger between supercritical fluid flows and solid walls.
The recovery temperature should be considered for the estimation of heat transfer between compressible flows and solid walls. For compressible flows on adiabatic airfoil surfaces, the local recovery temperature varies by each point on the airfoil surface, owing to the accelerating and decelerating effects of the main flow outside of the boundary layer on the airfoil surface. In addition, for compressible flows on cooling and heating airfoil surfaces, the local total temperature on airfoil surfaces in the boundary layer also varies at each point because of cooling and heating effects. The accelerating and decelerating effects can be estimated from the local Mach number distribution on the airfoil shape. The cooling and heating effects can also be estimated when a numerical integration of elapsed variation of the local total temperature along the boundary layer from the leading edge if the detailed solid temperature distribution on the airfoil surface is known. To obtain the detailed solid temperature distribution on the airfoil surface, detailed experimental measurements or an accurate CFD analysis may be required.
To estimate conjugate heat transfer through a practical heat exchanger with a complex shape, one solution is a combination of experimental results in wind tunnel tests and an inverse heat conduction method. The other solution is CFD analysis validated by experimental results in wind tunnel tests. Empirical correlations are very limited for conjugate heat transfer through a practical heat exchanger with complex shape because knowledge in this field is still developing.
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