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Thermal interface between a thermal liquid and its surroundings

Fluid Network Interfaces/Heat Exchangers/Fundamental Components

The Heat Exchanger Interface (TL) block models the pressure drop and temperature change between the thermal liquid inlet and outlet of a thermal interface. Combine with the E-NTU Heat Transfer block to model the heat transfer rate across the interface between two fluids.

The form of the mass balance equation depends on the dynamic
compressibility setting. If the **Fluid dynamic compressibility** parameter
is set to `Off`

, the mass balance equation
is

$${\dot{m}}_{A}+{\dot{m}}_{B}=0,$$

where:

*$${\dot{m}}_{A}$$*and*$${\dot{m}}_{B}$$*are the mass flow rates into the interface through ports A and B.

If the **Fluid dynamic compressibility** parameter
is set to `On`

, the mass balance equation
is

$${\dot{m}}_{A}+{\dot{m}}_{B}=\left(\frac{dp}{dt}\frac{1}{\beta}-\frac{dT}{dt}\alpha \right)\rho V,$$

where:

*p*is the pressure of the thermal liquid volume.*T*is the temperature of the thermal liquid volume.*α*is the isobaric thermal expansion coefficient of the thermal liquid volume.*β*is the isothermal bulk modulus of the thermal liquid volume.*ρ*is the mass density of the thermal liquid volume.*V*is the volume of thermal liquid in the heat exchanger interface.

The momentum balance in the heat exchanger interface depends
on the fluid dynamic compressibility setting. If the **Fluid dynamic compressibility** parameter is
set to `On`

, the momentum balance factors
in the internal pressure of the heat exchanger interface explicitly.
The momentum balance in the half volume between port A and the internal
interface node is computed as

$${p}_{A}-p=\Delta {p}_{\text{Loss,A}},$$

while in the half volume between port B and the internal interface node it is computed as

$${p}_{B}-p=\Delta {p}_{\text{Loss,B}},$$

where:

*p*_{A}and*p*_{B}are the pressures at ports A and B.*p*is the pressure in the internal node of the interface volume.*Δp*_{Loss,A}and*Δp*_{Loss,B}are the pressure losses between port A and the internal interface node and between port B and the internal interface node.

If the **Fluid dynamic compressibility** parameter
is set to `Off`

, the momentum balance in
the interface volume is computed directly between ports A and B as

$${p}_{A}-{p}_{B}=\Delta {p}_{Loss,A}-\Delta {p}_{Loss,B}.$$

The exact form of the pressure loss terms depends on the **Pressure
loss parameterization** setting in the block dialog box.
If the pressure loss parameterization is set to ```
Constant
loss coefficient
```

, the pressure loss in the half volume
adjacent to port A is

$$\Delta {p}_{Loss,A}=\{\begin{array}{ll}{\dot{m}}_{A}{\mu}_{A}{\left(CP\right)}_{Loss}{\mathrm{Re}}_{L}\frac{1}{4{D}_{h,p}{\rho}_{A}{S}_{Min}},\hfill & {\mathrm{Re}}_{A}\le {\mathrm{Re}}_{L}\hfill \\ {\left(CP\right)}_{Loss}\frac{{\dot{m}}_{A}\left|{\dot{m}}_{A}\right|}{4{\rho}_{A}{S}_{Min}^{2}},\hfill & {\mathrm{Re}}_{A}\ge {\mathrm{Re}}_{T}\hfill \end{array},$$

while in the half volume adjacent to port B it is

$$\Delta {p}_{Loss,B}=\{\begin{array}{ll}{\dot{m}}_{B}{\mu}_{B}{\left(CP\right)}_{Loss}{\mathrm{Re}}_{L}\frac{1}{4{D}_{h,p}{\rho}_{B}{S}_{Min}},\hfill & {\mathrm{Re}}_{B}\le {\mathrm{Re}}_{L}\hfill \\ {\left(CP\right)}_{Loss}\frac{{\dot{m}}_{B}\left|{\dot{m}}_{B}\right|}{4{\rho}_{B}{S}_{Min}^{2}},\hfill & {\mathrm{Re}}_{B}\ge {\mathrm{Re}}_{T}\hfill \end{array},$$

where:

*μ*_{A}and*μ*_{B}are the fluid dynamic viscosities at ports A and B.*CP*_{Loss}is the**Pressure loss coefficient**parameter specified in the block dialog box.*Re*_{L}is the Reynolds number upper bound for the laminar flow regime.*Re*_{T}is the Reynolds number lower bound for the turbulent flow regime.*D*_{h,p}is the hydraulic diameter for pressure loss calculations.*ρ*_{A}and*ρ*_{B}are the fluid mass densities at ports A and B.*S*_{Min}is the total minimum free-flow area.

If the pressure loss parameterization is set to ```
Correlations
for tubes
```

, the pressure loss in the half volume adjacent
to port A is

$$\Delta {p}_{Loss,A}=\{\begin{array}{ll}{\dot{m}}_{A}{\mu}_{A}\lambda \frac{\left({L}_{press}+{L}_{add}\right)}{4{D}_{h,p}{\rho}_{A}{S}_{Min}},\hfill & {\mathrm{Re}}_{A}\le {\mathrm{Re}}_{L}\hfill \\ {f}_{T,A}\frac{\left({L}_{press}+{L}_{add}\right)}{4{D}_{h,p}}\frac{{\dot{m}}_{A}\left|{\dot{m}}_{A}\right|}{{\rho}_{A}{S}_{Min}^{2}},\hfill & {\mathrm{Re}}_{A}\ge {\mathrm{Re}}_{T}\hfill \end{array},$$

while in the half volume adjacent to port B it is

$$\Delta {p}_{Loss,B}=\{\begin{array}{ll}{\dot{m}}_{B}{\mu}_{B}\lambda \frac{\left({L}_{press}+{L}_{add}\right)}{4{D}_{h,p}{\rho}_{B}{S}_{Min}},\hfill & {\mathrm{Re}}_{B}\le {\mathrm{Re}}_{L}\hfill \\ {f}_{T,B}\frac{\left({L}_{press}+{L}_{add}\right)}{4{D}_{h,p}}\frac{{\dot{m}}_{B}\left|{\dot{m}}_{B}\right|}{{\rho}_{B}{S}_{Min}^{2}},\hfill & {\mathrm{Re}}_{B}\ge {\mathrm{Re}}_{T}\hfill \end{array},$$

where:

*L*_{press}is the flow path length from inlet to outlet.*L*_{add}is the aggregate equivalent length of local resistances.*f*_{T,A}and*f*_{T,B}are the turbulent-regime Darcy friction factors at ports A and B.

The Darcy friction factor in the half volume adjacent to port A is

$${f}_{T,A}=\frac{1}{{\left[-1.8{\mathrm{log}}_{10}{\left(\frac{6.9}{{\mathrm{Re}}_{A}}+\frac{r}{3.7{D}_{h,p}}\right)}^{1.11}\right]}^{2}},$$

while in the half volume adjacent to port B it is

$${f}_{T,B}=\frac{1}{{\left[-1.8{\mathrm{log}}_{10}{\left(\frac{6.9}{{\mathrm{Re}}_{B}}+\frac{r}{3.7{D}_{h,p}}\right)}^{1.11}\right]}^{2}},$$

where:

*r*is the internal surface absolute roughness.

If the pressure loss parameterization is set to ```
Tabulated
data — Darcy friction factor vs. Reynolds number
```

,
the pressure loss in the half volume adjacent to port A is

$$\Delta {p}_{Loss,A}=\{\begin{array}{ll}{\dot{m}}_{A}{\mu}_{A}\lambda \frac{{L}_{press}}{4{D}_{h,p}^{2}{\rho}_{A}{S}_{Min}},\hfill & {\mathrm{Re}}_{A}\le {\mathrm{Re}}_{L}\hfill \\ f\left({\mathrm{Re}}_{A}\right)\frac{{L}_{press}}{4{D}_{h,p}}\frac{{\dot{m}}_{A}\left|{\dot{m}}_{A}\right|}{{\rho}_{A}{S}_{Min}^{2}},\hfill & {\mathrm{Re}}_{A}\ge {\mathrm{Re}}_{T}\hfill \end{array},$$

while in the half volume adjacent to port B it is

$$\Delta {p}_{Loss,B}=\{\begin{array}{ll}{\dot{m}}_{B}{\mu}_{B}\lambda \frac{{L}_{press}}{4{D}_{h,p}^{2}{\rho}_{B}{S}_{Min}},\hfill & {\mathrm{Re}}_{B}\le {\mathrm{Re}}_{L}\hfill \\ f\left({\mathrm{Re}}_{B}\right)\frac{{L}_{press}}{4{D}_{h,p}}\frac{{\dot{m}}_{B}\left|{\dot{m}}_{B}\right|}{{\rho}_{B}{S}_{Min}^{2}},\hfill & {\mathrm{Re}}_{B}\ge {\mathrm{Re}}_{T}\hfill \end{array},$$

where:

*λ*is the shape factor for laminar flow viscous friction.*f*(*Re*_{A}) and*f*(*Re*_{B}) are the Darcy friction factors at ports A and B. The block obtains the friction factors from tabulated data specified relative to the Reynolds number.

If the pressure loss parameterization is set to ```
Tabulated
data — Euler number vs. Reynolds number
```

, the
pressure loss in the half volume adjacent to port A is

$$\Delta {p}_{Loss,A}=\{\begin{array}{ll}{\dot{m}}_{A}{\mu}_{A}\text{Eu}\left({\mathrm{Re}}_{L}\right){\mathrm{Re}}_{L}\frac{1}{4{D}_{h,p}{\rho}_{A}{S}_{Min}},\hfill & {\mathrm{Re}}_{A}\le {\mathrm{Re}}_{L}\hfill \\ Eu\left({\mathrm{Re}}_{A}\right)\frac{{\dot{m}}_{A}\left|{\dot{m}}_{A}\right|}{{\rho}_{A}{S}_{Min}^{2}},\hfill & {\mathrm{Re}}_{A}\ge {\mathrm{Re}}_{T}\hfill \end{array},$$

while in the half volume adjacent to port B it is

$$\Delta {p}_{Loss,B}=\{\begin{array}{ll}{\dot{m}}_{B}{\mu}_{B}\text{Eu}\left({\mathrm{Re}}_{L}\right){\mathrm{Re}}_{L}\frac{1}{4{D}_{h,p}{\rho}_{B}{S}_{Min}},\hfill & {\mathrm{Re}}_{B}\le {\mathrm{Re}}_{L}\hfill \\ Eu\left({\mathrm{Re}}_{B}\right)\frac{{\dot{m}}_{B}\left|{\dot{m}}_{B}\right|}{{\rho}_{B}{S}_{Min}^{2}},\hfill & {\mathrm{Re}}_{B}\ge {\mathrm{Re}}_{T}\hfill \end{array},$$

where:

*Eu*(*Re*_{L}) is the Euler number at the Reynolds number upper bound for laminar flows.*Eu*(*Re*_{A}) and*Eu*(*Re*_{B}) are the Euler numbers at ports A and B. The block obtains the Euler numbers from tabulated data specified relative to the Reynolds number.

The energy balance in the heat exchanger interface depends on
the fluid dynamic compressibility setting. If the **Fluid
dynamic compressibility** parameter is set to `On`

,
the energy balance is

$$\frac{dp}{dt}\frac{dU}{dp}+\frac{dT}{dt}\frac{dU}{dT}={\varphi}_{A}+{\varphi}_{B}+{Q}_{H},$$

where:

*U*is the internal energy contained in the volume of the heat exchanger interface.*Φ*_{A}and*Φ*_{B}are the energy flow rates through ports**A**and**B**into the volume of the heat exchanger interface.*Q*_{H}is the heat flow rate through port**H**, representing the interface wall, into the volume of the heat exchange interface.

The internal energy derivatives are defined as

$$\frac{dU}{dp}=\left[\frac{1}{\beta}\left(\rho u+p\right)-T\alpha \right]V$$

and

$$\frac{dU}{dT}=\left[{c}_{p}-\alpha \left(u+\frac{p}{\rho}\right)\right]\rho V,$$

where *u* is the specific internal energy of the
thermal liquid, or the internal energy contained in a unit mass of the same.

If the **Fluid dynamic compressibility** parameter is set to
`Off`

, the thermal liquid density is treated as a
constant. The bulk modulus is then effectively infinite and the thermal expansion
coefficient zero. The pressure and temperature derivatives of the compressible case
vanish and the energy balance is restated as

$$\frac{dE}{dt}={\varphi}_{A}+{\varphi}_{B}+{Q}_{H},$$

where *E* is the total internal energy of the
incompressible thermal liquid, or

$$E=\rho uV.$$

The block calculates and outputs the liquid-wall heat transfer
coefficient value. The calculation depends on the **Heat transfer
coefficient specification** setting in the block dialog box.
If the heat transfer coefficient specification is ```
Constant
heat transfer coefficient
```

, the heat transfer coefficient
is simply the constant value specified in the block dialog box,

$${h}_{L-W}={h}_{Const},$$

where:

*h*_{L-W}is the liquid-wall heat transfer coefficient.*h*_{Const}is the**Liquid-wall heat transfer coefficient value**specified in the block dialog box.

For all other heat transfer coefficient parameterizations, the heat transfer coefficient is defined as the arithmetic average of the port heat transfer coefficients:

$${h}_{L-W}=\frac{{h}_{A}+{h}_{B}}{2},$$

where:

*h*_{A}and*h*_{B}are the liquid-wall heat transfer coefficients at ports A and B.

The heat transfer coefficient at port A is

$${h}_{A}=\frac{N{u}_{A}{k}_{A}}{{D}_{h,heat}},$$

while at port B it is

$${h}_{B}=\frac{N{u}_{B}{k}_{B}}{{D}_{h,heat}},$$

where:

*Nu*_{A}and*Nu*_{B}are the Nusselt numbers at ports A and B.*k*_{A}and*k*_{B}are the thermal conductivities at ports A and B.*D*_{h,heat}is the hydraulic diameter for heat transfer calculations.

The hydraulic diameter used in heat transfer calculations is defined as

$${D}_{h,heat}=\frac{4{S}_{Min}{L}_{heat}}{{S}_{heat}},$$

where:

*L*_{heat}is the flow path length used in heat transfer calculations.*S*_{heat}is the total heat transfer surface area.

The Nusselt number calculation depends on the **Heat
transfer coefficient specification** setting in the block
dialog box. If the heat transfer specification is set to ```
Correlations
for tubes
```

, the Nusselt number at port A is

$$N{u}_{A}=\{\begin{array}{ll}{\text{Nu}}_{L},\hfill & {\mathrm{Re}}_{A}\le {\mathrm{Re}}_{L}\hfill \\ \frac{\left(\raisebox{1ex}{${f}_{T,A}$}\!\left/ \!\raisebox{-1ex}{$8$}\right.\right)\left({\mathrm{Re}}_{A}-1000\right){\mathrm{Pr}}_{A}}{1+12.7{\left(\raisebox{1ex}{${f}_{T,A}$}\!\left/ \!\raisebox{-1ex}{$8$}\right.\right)}^{1/2}\left({\mathrm{Pr}}_{B}^{2/3}-1\right)},\hfill & {\mathrm{Re}}_{A}\ge {\mathrm{Re}}_{T}\hfill \end{array},$$

while at port B it is

$$N{u}_{B}=\{\begin{array}{ll}{\text{Nu}}_{L},\hfill & {\mathrm{Re}}_{B}\le {\mathrm{Re}}_{L}\hfill \\ \frac{\left(\raisebox{1ex}{${f}_{T,B}$}\!\left/ \!\raisebox{-1ex}{$8$}\right.\right)\left({\mathrm{Re}}_{B}-1000\right){\mathrm{Pr}}_{B}}{1+12.7{\left(\raisebox{1ex}{${f}_{T,B}$}\!\left/ \!\raisebox{-1ex}{$8$}\right.\right)}^{1/2}\left({\mathrm{Pr}}_{B}^{2/3}-1\right)},\hfill & {\mathrm{Re}}_{B}\ge {\mathrm{Re}}_{T}\hfill \end{array},$$

where:

*Nu*_{L}is the**Nusselt number for laminar flow heat transfer**value specified in the block dialog box.*Pr*_{A}and*Pr*_{B}are the Prandtl numbers at ports A and B.

If the heat transfer specification is set to ```
Tabulated
data — Colburn data vs. Reynolds number
```

, the
Nusselt number at port A is

$$N{u}_{A}=j\left({\mathrm{Re}}_{A,heat}\right){\mathrm{Re}}_{A,heat}{\mathrm{Pr}}_{A}^{1/3},$$

while at port B it is

$$N{u}_{B}=j\left({\mathrm{Re}}_{B,heat}\right){\mathrm{Re}}_{B,heat}{\mathrm{Pr}}_{B}^{1/3},$$

where:

*j*(*Re*_{A,heat}) and*j*(*Re*_{B,heat}) are the Colburn numbers at ports A and B. The block obtains the Colburn numbers from tabulated data provided as a function of the Reynolds number.*Re*_{A,heat}and*Re*_{B,heat}are the Reynolds numbers based on the hydraulic diameters for heat transfer calculations at ports A and B. This parameter is defined at port A as$${\mathrm{Re}}_{A,heat}=\frac{{\dot{m}}_{A}{D}_{h,heat}}{{S}_{Min}{\mu}_{A}},$$

and at port B as

$${\mathrm{Re}}_{B}=\frac{{\dot{m}}_{B}{D}_{h,heat}}{{S}_{Min}{\mu}_{B}}.$$

If the heat transfer specification is set to ```
Tabulated
data — Nusselt number vs. Reynolds number & Prandtl number
```

,
the Nusselt number at port A is

$$N{u}_{A}=Nu\left({\mathrm{Re}}_{A,heat},{\mathrm{Pr}}_{A}\right),$$

while at port B it is

$$N{u}_{B}=Nu\left({\mathrm{Re}}_{B,heat},{\mathrm{Pr}}_{B}\right).$$

The hydraulic diameter used in heat transfer calculations can differ from the hydraulic diameter employed in pressure loss calculations, and are different if the heated and friction perimeters are not the same. For a concentric pipe heat exchanger with an annular cross-section, the hydraulic diameter for heat transfer calculations is

$${D}_{h,heat}=\frac{4\left(\pi /4\right)\left({D}_{o}^{2}-{D}_{i}^{2}\right)}{\pi {D}_{i}}=\frac{{D}_{o}^{2}-{D}_{i}^{2}}{{D}_{i}},$$

while the hydraulic diameter for pressure calculations is

$${D}_{h,p}=\frac{4\left(\pi /4\right)\left({D}_{o}^{2}-{D}_{i}^{2}\right)}{\pi \left({D}_{i}+{D}_{o}\right)}={D}_{o}-{D}_{i},$$

where:

*D*_{o}is the outer annulus diameter.*D*_{i}is the inner annulus diameter.

**Annulus Schematic**

**Minimum free-flow area**Aggregate flow area free of obstacles based on the smallest tube spacing or corrugation pitch. The default value is

`0.01`

m^2.**Hydraulic diameter for pressure loss**Hydraulic diameter of the tubes or channels comprising the heat exchange interface. The hydraulic diameter is the ratio of the flow cross-sectional area to the channel perimeter . The default value is

`0.1`

m.**Laminar flow upper Reynolds number limit**Reynolds number corresponding to the upper bound of the laminar flow regime. The flow transitions to turbulent above this value. The default value is

`2000`

.**Turbulent flow lower Reynolds number limit**Reynolds number corresponding to the lower bound of the turbulent flow regime. The flow transitions to laminar below this value. The default value is

`4000`

.**Pressure loss parameterization**Parameterization used to compute the pressure loss between the inlet and outlet. You can assume a constant loss coefficient, use empirical correlations for tubes, or specify tabulated data for the Darcy friction factor or the Euler number. The default setting is

`Constant loss coefficient`

.**Pressure loss coefficient**Dimensionless number used to compute the pressure loss between the inlet and outlet. The pressure loss coefficient is assumed constant and the same for direct and reverse flows. This parameter is visible only if the

**Pressure loss parameterization**parameter is set to`Constant loss coefficient`

. The default value is`.1`

.**Length of flow path from inlet to outlet**Distance traversed by the fluid from inlet to outlet. This parameter is visible only if the

**Pressure loss parameterization**parameter is set to`Correlations for tubes`

or`Tabulated data — Darcy friction factor vs. Reynolds number`

. The default value is`1`

m.**Aggregate equivalent length of local resistances**Pressure loss due to local resistances such as bends, inlets, and fittings, expressed as the equivalent length of those resistances. This parameter is visible only if the

**Pressure loss parameterization**parameter is set to`Correlations for tubes`

. The default value is`0.1`

m.**Internal surface absolute roughness**Average height of all surface defects on the internal surface of the pipe. The surface roughness enables the calculation of the friction factor in the turbulent flow regime. This parameter is visible only if the

**Pressure loss parameterization**parameter is set to`Correlations for tubes`

. The default value is`15e-6`

m.**Shape factor for laminar flow viscous friction**Proportionality constant between convective and conductive heat transfer in the laminar regime. The shape factor encodes the effects of component geometry on the laminar friction losses. This parameter is visible only if the

**Pressure loss parameterization**parameter is set to`Correlations for tubes`

. The default value is`64`

.**Reynolds number vector for Darcy friction factor**M-element vector of Reynolds numbers at which to specify the Darcy friction factor. The block uses this vector to create a lookup table for the Darcy friction factor. This parameter is visible only if the

**Pressure loss parameterization**parameter is set to`Tabulated data — Darcy friction factor vs. Reynolds number`

. The default vector is a 12–element vector ranging in value from`400`

to`1e8`

.**Darcy friction factor vector**M-element vector of Darcy friction factors corresponding to the values specified in the

**Reynolds number vector for Darcy friction factor**parameter. The block uses this vector to create a lookup table for the Darcy friction factor. This parameter is visible only if the**Pressure loss parameterization**parameter is set to`Tabulated data — Darcy friction factor vs. Reynolds number`

. The default vector is a 12-element vector ranging in value from`0.0214`

to`0.2640`

.**Reynolds number vector for Euler number**M-element vector of Reynolds numbers at which to specify the Euler number. The block uses this vector to create a lookup table for the Euler number. This parameter is visible only if the

**Pressure loss parameterization**parameter is set to`Tabulated data — Euler number vs. Reynolds number`

.**Euler number vector**M-element vector of Euler numbers corresponding to the values specified in the

**Reynolds number vector for Euler number**parameter. The block uses this vector to create a lookup table for the Euler number. This parameter is visible only if the**Pressure loss parameterization**parameter is set to`Tabulated data — Euler number vs. Reynolds number`

.**Heat transfer parameterization**Parameterization used to compute the heat transfer rate between the heat exchanger fluids. You can assume a constant loss coefficient, use empirical correlations for tubes, or specify tabulated data for the Colburn or Nusselt number. The default setting is

`Constant loss coefficient`

.**Heat transfer surface area**Aggregate surface area available for heat transfer between the heat exchanger fluids. This parameter is visible only when the

**Heat transfer parameterization**parameter is set to`Correlation for tubes`

,`Tabulated data — Colburn factor vs. Reynolds number`

, or`Tabulated data — Nusselt number vs. Reynolds number & Prandtl number`

. The default value is`0.4`

m^2.**Liquid-wall heat transfer coefficient**Heat transfer coefficient between the thermal liquid and the heat-transfer surface. This parameter is visible only when the

**Heat transfer parameterization**parameter is set to`Constant heat transfer coefficient`

. The default value is`100`

.**Length of flow path for heat transfer**Distance traversed by the fluid along which heat exchange takes place. This parameter is visible only when the

**Heat transfer parameterization**parameter is set to`Correlation for tubes`

,`Tabulated data — Colburn factor vs. Reynolds number`

, or`Tabulated data — Nusselt number vs. Reynolds number & Prandtl number`

. The default value is`1`

m.**Nusselt number for laminar flow heat transfer**Proportionality constant between convective and conductive heat transfer in the laminar regime. This parameter enables the calculation of convective heat transfer rates in laminar flows. The appropriate value to use depends on component geometry. This parameter is visible only when the

**Heat transfer parameterization**parameter is set to`Correlation for tubes`

. The default value is`3.66`

.**Reynolds number vector for Colburn factor**M-element vector of Reynolds numbers at which to specify the Colburn factor. The block uses this vector to create a lookup table for the Colburn number. This parameter is visible only when the

**Heat transfer parameterization**parameter is set to`Tabulated data — Colburn factor vs. Reynolds number`

. The default vector is`[100.0, 150.0, 1000.0]`

.**Colburn factor vector**M-element vector of Colburn factors corresponding to the values specified in the

**Reynolds number vector for Colburn number**parameter. The block uses this vector to create a lookup table for the Colburn factor. This parameter is visible only when the**Heat transfer parameterization**parameter is set to`Tabulated data — Colburn factor vs. Reynolds number`

. The default vector is`[0.019, 0.013, 0.002]`

.**Reynolds number vector for Nusselt number**M-element vector of Reynolds numbers at which to specify the Nusselt number. The block uses this vector to create a lookup table for the Nusselt number. This parameter is visible only when the

**Heat transfer parameterization**parameter is set to`Tabulated data — Nusselt number vs. Reynolds number & Prandtl number`

. The default vector is`[100.0, 150.0, 1000.0]`

.**Prandtl number vector for Nusselt number**N-element vector of Prandtl numbers at which to specify the Nusselt number. The block uses this vector to create a lookup table for the Nusselt number. This parameter is visible only when the

**Heat transfer parameterization**parameter is set to`Tabulated data — Nusselt number vs. Reynolds number & Prandtl number`

. The default vector is [1.0, 10.0].**Nusselt number table, Nu(Re,Pr)**M-by-N matrix of Nusselt numbers corresponding to the values specified in the

**Reynolds number vector for Nusselt number**and**Prandtl number vector for Nusselt number**parameters. The block uses this vector to create a lookup table for the Nusselt factor. This parameter is visible only when the**Heat transfer parameterization**parameter is set to`Tabulated data — Nusselt number vs. Reynolds number & Prandtl number`

. The default matrix is`[3.72, 4.21; 3.75, 4.44; 4.21, 7.15]`

.**Fouling factor**Empirical parameter used to quantify the increased thermal resistance due to dirt deposits on the heat transfer surface. The default value is

`1e-4`

m^2*K/W.

**Thermal Liquid dynamic compressibility**Option to model the pressure dynamics inside the heat exchanger. Setting this parameter to

`Off`

removes the pressure derivative terms from the component energy and mass conservation equations. The pressure inside the heat exchanger is then reduced to the weighted average of the two port pressures.**Thermal Liquid initial temperature**Temperature of the internal volume of thermal liquid at the start of simulation.

**Thermal Liquid initial pressure**Pressure of the internal volume of thermal liquid at the start of simulation.

A — Thermal liquid conserving port representing the thermal liquid inlet

B — Thermal liquid conserving port representing the thermal liquid outlet

C — Physical signal output port for the thermal capacity rate of the thermal liquid

H — Thermal conserving port associated with the thermal liquid inlet temperature

HC — Physical signal output port for the heat transfer coefficient between the thermal liquid and the interface wall