# Heat Exchanger Interface (G)

Gas side of heat exchanger

• Library:
• Simscape / Fluids / Fluid Network Interfaces / Heat Exchangers / Fundamental Components

• ## Description

The Heat Exchanger Interface (G) block models thermal transfer by a gaseous flow within a heat exchanger. Use a second heat exchanger block to model the fluid pair. The interfaces can be in different fluid domains, such as one in liquid and one in gas. Use an E-NTU Heat Transfer block to couple the interfaces and capture the heat exchange between the fluids.

### Mass Balance

The fixed-volume construction of the block allows you to capture variations in fluid mass flow rates due to compressibility. The overall mass accumulation rate is equal to the sum of the mass flow rates through the ports:

`$\stackrel{˙}{M}={\stackrel{˙}{m}}_{\text{A}}+{\stackrel{˙}{m}}_{\text{B}},$`

where $\stackrel{˙}{M}$ is the mass accumulation rate and $\stackrel{˙}{m}$ is the mass flow rate. The subscripts denote ports A and B. The mass flow rate is positive when it is directed into the gas channel. Variations in density are reflected in the mass accumulation rate:

`$\stackrel{˙}{M}=\left[{\left(\frac{\partial \rho }{\partial p}\right)}_{u}\frac{dp}{dt}+{\left(\frac{\partial \rho }{\partial u}\right)}_{p}\frac{du}{dt}\right]V,$`

where:

• ρ is density.

• p is pressure.

• u is specific internal energy.

• V is volume.

### Momentum Balance

Balancing momentum between the inlet and outlet ports of the heat exchanger dictates the flow direction and speed within the exchanger. Changes in momentum are due primarily due to friction losses from pipe turns, which translate to changes in pressure. Local resistances, such as bends, elbows, and tees can result in flow separation that leads to minor additional pressure losses. For steady flows, the mass flow rate remains constant.

A momentum balance is applied to each segment of the gas (pipe) volume. This figure shows a tube bank divided into two volumes and three nodes. The nodes correspond to ports A , B, and the fluid volume, `I`. Fluid states, such as pressure and temperature, and fluid properties, such as density and viscosity, are defined at these nodes. Note that flow inertia is negligible and the flow is considered to be quasi-steady state. The translation of transients to mass flow rates can be offset: due to coupling between density, pressure, and temperature, propagation of changes throughout the system is not instantaneous. Other sources and sinks of momentum, such as differences in head between ports or radial deformations of the channel wall, are not considered. The momentum balance for the half volume at port A is:

`${p}_{\text{A}}-{p}_{\text{I}}=\Delta {p}_{\text{f,A}},$`

where p is the pressure at the node indicated in the subscript. Δpf,A is the total pressure loss between the port node and the internal node due to friction. The total pressure loss includes both major and minor losses. For the half volume at port B, the momentum balance is:

`${p}_{\text{B}}-{p}_{\text{I}}=\Delta {p}_{\text{f,B}}.$`

### Friction

Pressure changes due to friction vary with the square of the mass flow rate for turbulent flows and with the magnitude of the mass flow rate for laminar flows. This pressure change is characterized by three dimensionless parameters: the Darcy friction factor, the pressure loss coefficient, and the Euler number. These numbers are calculated from empirical correlations or are estimated from lookup tables, depending on the Pressure loss parameterization parameter.

Classification of "laminar" or "turbulent" flow is based on the Reynolds number. When the Reynolds number is above the Turbulent flow lower Reynolds number limit parameter, the flow is fully turbulent. Below the Laminar flow upper Reynolds number limit parameter, the flow is fully laminar. Reynolds numbers in between these values indicate transitional flow. Transitional flows show characteristics of both laminar and turbulent flows. In the Simscape™ Fluids™ language, numerical blending is applied between these bounding values.

`Correlations for tubes`

For tubes, the Darcy friction factor, fD, is used. In the half volume at port A, the momentum balance is:

`${p}_{A}-{p}_{\text{I}}=\frac{{f}_{\text{D,A}}{\stackrel{˙}{m}}_{\text{A}}|{\stackrel{˙}{m}}_{\text{A}}|}{2{\rho }_{\text{A}}{D}_{\text{H}}{A}_{\text{Min}}^{2}}\left(\frac{L+{L}_{\text{Add}}}{2}\right),$`

where L is the tube length and LAdd is the added tube length that would reproduce the minor viscous losses if used in place of elbows, tees, unions, or other local resistances. A is the tube cross-sectional area; in the event of a non-uniform cross-sectional area, Amin should be used. DH is the tube hydraulic diameter, or the diameter of a circle equal in area to the tube cross section:

`${D}_{\text{H}}=\sqrt{\frac{4{A}_{\text{Min}}}{\pi }}.$`

If the tube has a circular cross section, the hydraulic diameter and the tube diameter are the same.

For the half volume at port B, the momentum balance is:

`${p}_{\text{B}}-{p}_{\text{I}}=\frac{{f}_{\text{D,B}}{\stackrel{˙}{m}}_{\text{B}}|{\stackrel{˙}{m}}_{\text{B}}|}{2{\rho }_{\text{B}}{D}_{\text{H}}{A}_{\text{Min}}^{2}}\left(\frac{L+{L}_{\text{Add}}}{2}\right).$`

For turbulent flows, the Darcy friction factor is calculated with the Haaland correlation. The Reynolds number is established at the bounding port:

`${f}_{\text{D}}={\left\{-1.8{\text{log}}_{\text{10}}\left[\frac{6.9}{\text{Re}}+{\left(\frac{{ϵ}_{\text{R}}}{3.7{D}_{\text{H}}}\right)}^{1.11}\right]\right\}}^{\text{-2}},$`

where εR is wall roughness, taken as a characteristic height. This parameter is specified in the Internal surface absolute roughness parameter.

For laminar flows, the friction factor depends on the tube shape and is calculated with the tube shape factor:

`${f}_{\text{D}}=\frac{\lambda }{\text{Re}},$`

where λ is the shape factor. The Reynolds number is calculated at the bounding port as:

`$\text{Re}=\frac{{D}_{\text{H}}\stackrel{˙}{m}}{\mu {A}_{\text{Min}}}.$`

Substituting Re into the pressure loss equation at port A, the momentum balance is reformulated as:

`${p}_{\text{A}}-{p}_{\text{I}}=\frac{{\lambda }_{\text{A}}{\mu }_{\text{A}}{\stackrel{˙}{m}}_{\text{A}}}{2{\rho }_{\text{A}}{D}_{\text{H}}^{2}{A}_{\text{Min}}}\left(\frac{L+{L}_{\text{Add}}}{2}\right),$`

Likewise, for the half volume at port B, the momentum balance is:

`${p}_{\text{B}}-{p}_{\text{I}}=\frac{{\lambda }_{\text{B}}{\mu }_{\text{B}}{\stackrel{˙}{m}}_{\text{B}}}{2{\rho }_{\text{B}}{D}_{\text{H}}^{2}{A}_{\text{Min}}}\left(\frac{L+{L}_{\text{Add}}}{2}\right).$`

Using the constant loss coefficient

For channels other than tubes, use the pressure loss coefficient, ξ. For turbulent flows in the half volume at port A, the momentum balance is:

`${p}_{\text{A}}-{p}_{\text{I}}=\frac{1}{2}\xi \frac{{\stackrel{˙}{m}}_{\text{A}}|{\stackrel{˙}{m}}_{\text{A}}|}{2{\rho }_{\text{A}}{A}_{\text{Min}}^{2}},$`

For turbulent flows in the half volume at port B, the momentum balance is:

`${p}_{\text{B}}-{p}_{\text{I}}=\frac{1}{2}\xi \frac{{\stackrel{˙}{m}}_{\text{B}}|{\stackrel{˙}{m}}_{\text{B}}|}{2{\rho }_{\text{B}}{A}_{\text{Min}}^{2}},$`

For laminar flows in the half volume at port A, the momentum balance is:

`${p}_{\text{A}}-{p}_{\text{I}}=\frac{1}{2}\xi {\text{Re}}_{\text{L}}\frac{{\stackrel{˙}{m}}_{\text{A}}{\mu }_{\text{A}}}{2{D}_{\text{H}}{\rho }_{\text{A}}{A}_{\text{Min}}},$`

where ReL is the Laminar flow upper Reynolds number limit block parameter. For laminar flows in the half volume at port B, the momentum balance is:

`${p}_{\text{B}}-{p}_{\text{I}}=\frac{1}{2}\xi {\text{Re}}_{\text{L}}\frac{{\stackrel{˙}{m}}_{\text{B}}{\mu }_{\text{B}}}{2{D}_{\text{H}}{\rho }_{\text{B}}{A}_{\text{Min}}}$`

Using ```Tabulated data - Darcy friction factor vs. Reynolds number```

You can use tabulated data to determine the Darcy friction factor based on the Reynolds number for tube flows. For the half volume at port A, the momentum balance is:

`${p}_{\text{A}}-{p}_{\text{I}}=\frac{{f}_{\text{D,A}}{\stackrel{˙}{m}}_{\text{A}}|{\stackrel{˙}{m}}_{\text{A}}|}{2{\rho }_{\text{A}}{D}_{\text{H}}{A}_{\text{Min}}^{2}}\left(\frac{L+{L}_{\text{Add}}}{2}\right).$`

For the half volume at port B, the momentum balance is:

`${p}_{\text{B}}-{p}_{\text{I}}=\frac{{f}_{\text{D,B}}{\stackrel{˙}{m}}_{\text{B}}|{\stackrel{˙}{m}}_{\text{B}}|}{2{\rho }_{\text{B}}{D}_{\text{H}}{A}_{\text{Min}}^{2}}\left(\frac{L+{L}_{\text{Add}}}{2}\right).$`

For the turbulent regime, the friction factor is determined from a tabulated function of the Reynolds number:

`${f}_{\text{D}}={f}_{\text{D}}\left(\text{Re}\right).$`

The breakpoints of the tabulated function derive from the vector block parameters. The Reynolds number vector for Darcy friction factor parameter specifies the independent variable and the Darcy friction factor vector parameter specifies the dependent variable. Linear interpolation is applied between breakpoints. Outside of the tabulated data range, the nearest breakpoint determines the friction factor.

In the laminar regime, the friction factor is calculated from the shape factor, λ:

`${f}_{\text{D}}=\frac{\lambda }{\text{Re}}.$`

Using ```Tabulated data - Euler number vs. Reynolds number```

You can use tabulated data to determine the Euler number based on the Reynolds number. This calculation is dependent on flow regime, and the Euler number is formulated as a tabulated function of the Reynolds number:

`$\text{Eu}=\text{Eu}\left(\text{Re}\right).$`

The breakpoints in ```Tabulated data - Euler number vs. Reynolds number``` are specified by Reynolds number and Euler number vectors. The Reynolds number vector for Euler number parameter specifies the independent variables, the Reynolds numbers, and the Euler number vector parameter specifies the dependent variable, the Euler number, at each Reynolds number. Linear interpolation is used to determine values between breakpoints. Outside of the tabulated data range, the value at the nearest breakpoint is used.

For turbulent flows, the momentum balance for the half volume at port A is:

`${p}_{\text{A}}-{p}_{\text{I}}={\text{Eu}}_{\text{A}}\frac{{\stackrel{˙}{m}}_{\text{A}}|{\stackrel{˙}{m}}_{\text{A}}|}{{\rho }_{\text{A}}{A}_{\text{Min}}^{2}},$`

where Eu is the Euler number at port A. For turbulent flows, the momentum balance for the half volume at port B is:

`${p}_{\text{B}}-{p}_{\text{I}}={\text{Eu}}_{\text{A}}\frac{{\stackrel{˙}{m}}_{\text{B}}|{\stackrel{˙}{m}}_{\text{B}}|}{{\rho }_{\text{B}}{A}_{\text{Min}}^{2}}.$`

For laminar flow in the half volume at port A, the momentum balance is:

`${p}_{\text{A}}-{p}_{\text{I}}={\text{Eu}}_{\text{L}}{\text{Re}}_{\text{L}}\frac{{\stackrel{˙}{m}}_{\text{A}}{\mu }_{\text{A}}}{4{D}_{\text{H}}{\rho }_{\text{A}}{A}_{\text{Min}}},$`

where ReL is the Laminar flow upper Reynolds number limit parameter and EuL is the Euler number evaluated from tabulated data at that Reynolds number. For laminar flow in the half volume at port B, the momentum balance is:

`${p}_{\text{B}}-{p}_{\text{I}}={\text{Eu}}_{\text{L}}{\text{Re}}_{\text{L}}\frac{{\stackrel{˙}{m}}_{\text{B}}{\mu }_{\text{B}}}{4{D}_{\text{H}}{\rho }_{\text{B}}{A}_{\text{Min}}},$`

### Energy Balance

The energy balance within the gas volume is the sum of its flow rates across channel boundaries and the associated heat transfer. Energy can be transferred by advection at the ports and by convection at the wall. While conduction contributes to the energy balance at the ports, it is often negligible in comparison to advection. However, conduction is non-negligible in near-stationary fluids, such as when fluids are stagnant or changing direction. The energy balance equation is:

`${\stackrel{˙}{E}}_{\text{2P}}={\varphi }_{\text{A}}+{\varphi }_{\text{B}}+Q,$`

where:

• $\frac{\partial U}{\partial p}$ is the partial derivative of the internal energy of the gas volume with respect to pressure at constant temperature and volume.

• pI is the pressure of the gas volume.

• $\frac{\partial U}{\partial T}$ is the partial derivative of the internal energy of the gas volume with respect to temperature at constant pressure and volume.

• TI is the temperature of the gas volume.

• ΦA and ΦB are energy flow rates at ports A and B, respectively.

• Q is the heat transfer rate.

Advection and conduction are accounted for in Φ, and convection is accounted for in Q. The heat transfer rate is positive when directed into the gas volume.

### Heat Transfer Rate

Heat transfer between the two heat exchanger fluids occurs in multiple ways: through convection at the fluid interfaces, conduction through layers of built-up fouling, and conduction through the thickness of the wall.

Heat transfer extends beyond the gas channel and therefore requires other blocks to model the entire heat exchanger system. A second heat exchanger interface block models the second flow channel while an E-NTU Heat Transfer block models the heat flow across the wall. Heat transfer parameters that are specific to the gas channel, but required by the E-NTU Heat Transfer block, are available through the physical signal ports:

• Port C outputs the heat capacity rate, which is a measure of the gas' ability to absorb heat and is required for calculating the number of heat transfer units (NTU). The heat capacity rate is calculated as:

`${C}_{\text{R}}={c}_{\text{p}}\stackrel{˙}{m},$`

where CR is the heat capacity rate and cp is the specific heat.

• Port HC outputs the heat transfer coefficient, U.

If the heat transfer coefficient is treated as a constant, its value is uniform across the flow channel. If the heat transfer coefficient is variable, it is calculated at each port from the expression:

`$U=\frac{\text{Nu}k}{{D}_{\text{H,Q}}},$`

where Nu is Nusselt number, k is thermal conductivity, and DH,Q is a hydraulic diameter for heat transfer. The hydraulic diameterDH,Q is calculated as:

`${D}_{\text{H,Q}}=\frac{4{A}_{\text{Min}}{L}_{\text{Q}}}{{S}_{\text{Q}}},$`

where SQ is the Heat transfer surface area parameter and LQ is the Length of flow path for heat transfer parameter.

The lower bound of the mean heat transfer coefficient is the Minimum gas-wall heat transfer coefficient parameter.

### Nusselt Number

The Nusselt number is derived from empirical correlations with the Reynolds and Prandtl numbers. Use the Heat transfer parametrization parameter to select the most appropriate formulation for your simulation.

The simplest parameterization, ```Constant heat transfer coefficient```, obtains the heat transfer coefficient directly from the value of the Gas-wall heat transfer coefficient parameter. `Correlations for tubes` uses analytical expressions with constant or calculated parameters to capture Nusselt number dependence on the flow regime for tube flows.

The remaining parameterizations are tabulated functions of the Reynolds number. These are useful for varying Nusselt numbers, or heat transfer coefficients, across flow regimes. The functions are generated from experimental data relating the Reynolds number to the Colburn factor or the Reynolds and Prandtl numbers to the Nusselt number.

`Constant heat transfer coefficient`

Using `Constant heat transfer coefficient`, specified in the Gas-wall heat transfer coefficient parameter, sets the heat transfer coefficient as a constant, and does not use the Nusselt number in calculations. Use this parameterization as a simple approximation for gas flows confined to the laminar regime.

`Correlation for tubes`

The Nusselt number depends on flow regime when using ```Correlation for tubes```. For turbulent flows, its value changes in proportion to the Reynolds number and is calculated from the Gnielinski correlation:

`$\text{Nu}=\frac{\frac{f}{8}\left(\text{Re}-1000\right)\text{Pr}}{1+12.7\sqrt{\frac{f}{8}\left({\text{Pr}}^{2/3}-1\right)}},$`

where Re is the Reynolds number, Nu is the Nusselt number, and Pr is the Prandtl number. The friction factor, f, is the same as the factor used in tube pressure loss calculations. For laminar flows, the Nusselt number is a constant. Its value is obtained from the Nusselt number for laminar flow heat transfer parameter, NuL:

`$\text{Nu}={\text{Nu}}_{\text{L}}.$`

Using ```Tabulated data - Colburn factor vs. Reynolds number```

You can use tabulated data to determine the Colburn factor based on the Reynolds number. The Colburn equation is used to determine the Nusselt number, which varies in proportion to the Reynolds number. The Colburn j-factor is a measure of proportionality between the Reynolds, Prandtl, and Nusselt numbers:

`$\text{Nu}=j\left({\text{Re}}_{\text{Q}}\right){\text{Re}}_{\text{Q}}{\text{Pr}}^{1/3}.$`

ReQ is the Reynolds number based on the hydraulic diameter for heat transfer, DH, Q, and from the minimum free-flow area of the channel, AMin:

`${\text{Re}}_{\text{Q}}=\frac{\stackrel{˙}{m}{D}_{\text{H,Q}}}{{A}_{\text{Min}}\mu }$`

Using ```Tabulated data - Nusselt number vs. Reynolds number & Prandtl number```

You can use a tabulated function to determine the Nusselt number from the Prandtl and Reynolds numbers. Linear interpolation is used to determine values between breakpoints. The Nusselt number is a function of both Re and Pr, and therefore the Reynolds number vector for Nusselt number, Prandtl number vector for Nusselt number, and Nusselt number table, Nu(Re,Pr) parameters define the table breakpoints:

`$\text{Nu}=\text{Nu}\left({\text{Re}}_{\text{Q}},\text{Pr}\right).$`

The tabulated Reynolds number must be calculated using the hydraulic diameter for heat transfer, DH,Q.

## Ports

### Conserving

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Entry or exit point on the gas side of the heat exchanger.

Entry or exit point on the gas side of the heat exchanger.

Thermal boundary between the modeled fluid and the heat exchanger interface.

### Input

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Instantaneous value of the heat capacity rate for the gas flow, specified as a physical signal.

Instantaneous value of the heat transfer coefficient between gas flow and the wall, specified as a physical signal.

## Parameters

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Parameters Tab

Cross-sectional area of the flow channel at its narrowest point. If the channel is a collection of ducts, tubes, slots, or grooves, this area is the sum of the areas in the collection, minus the blockage due to walls, ridges, plates, or other barriers.

Effective inner diameter of the flow. If the diameter of the cross-section varies, the value of this parameter is the diameter at its narrowest point. For non-circular channels, the hydraulic diameter is the equivalent diameter of a circle with the same area of the existing channel.

If the channel is a collection of ducts, tubes, slots, or grooves, the gross perimeter is the sum of the perimeters in the collection. If the channel is a single pipe or tube that has a circular cross section, the hydraulic diameter is equal to the true diameter.

Total volume of the fluid contained in the gas or thermal liquid flow channel.

Start of the transition from the laminar regime to the turbulent regime. Above this number, inertial forces become increasingly dominant. The default value is given for circular pipes and tubes with smooth surfaces.

End of the transition from the laminar regime to the turbulent regime. Below this number, viscous forces become increasingly dominant. The default value is for circular pipes and tubes with smooth surfaces.

Mathematical model for pressure loss due to friction. This setting determines which expressions to use for calculation and which block parameters to specify as input. See the Heat Exchanger Interface (TL) blocks for the calculations by parameterization.

Aggregate loss coefficient for all flow resistances in the flow channel, including wall friction (major losses) and local resistances due to bends, elbows, and other geometry changes (minor losses).

The loss coefficient is an empirical, dimensionless number used to express the pressure losses due to friction. It can be calculated from experimental data or obtained from product data sheets.

#### Dependencies

To enable this parameter, set Pressure loss parameterization to ```Constant loss coefficient```.

Total distance the flow must travel between the ports. In multi-pass shell-and-tube exchangers, the total distance is the sum over all shell passes. In tube bundles, corrugated plates, and other channels where the flow is split into parallel branches, it is the distance covered in a single branch. The longer the flow path, the steeper the major pressure loss due to friction at the wall.

#### Dependencies

To enable this parameter, set Pressure loss parameterization to ```Correlations for tubes``` or ```Tabulated data - Darcy friction factor vs Reynolds number```.

Aggregate minor pressure loss, expressed as a length. The length of a straight channel results in equivalent losses to the sum of existing local resistances from elbows, tees, and unions. The larger the equivalent length, the steeper the minor pressure loss due to the local resistances.

#### Dependencies

To enable this parameter, set Pressure loss parameterization to ```Correlations for tubes```.

Mean height of the wall surface variations that contribute to frictional losses. The greater the mean height, the rougher the wall and the larger the pressure loss due to friction. Surface roughness is required to derive the Darcy friction factor from the Haaland correlation.

#### Dependencies

To enable this parameter, set Pressure loss parameterization to ```Correlations for tubes```.

Pressure loss correction for laminar flow. This parameter is referred to as the shape factor, and can be used to derive the Darcy friction factor for pressure loss calculations in the laminar regime. The default value is for cylindrical pipes and tubes.

Some additional shape factors for non-circular cross-sections can be determined from analytical solutions to the Navier-Stokes equations. A square duct has a shape factor of `56`, a rectangular duct with an aspect ratio of 2:1 has a shape factor of `62`, and an annular tube has a shape factor of `96`. A slender conduit between parallel plates also has a shape factor of `96`.

#### Dependencies

To enable this parameter, set Pressure loss parameterization to ```Correlations for tubes```.

Reynolds number at each breakpoint in the lookup table for the Darcy friction factor. The block interpolates between and extrapolates from the breakpoints to obtain the Darcy friction factor at any Reynolds number. Interpolation is handled by the MATLAB® `linear` estimator and extrapolation is handled by the `nearest` function.

The Reynolds numbers must be greater than zero and increase monotonically from left to right. They can span across laminar, transient, and turbulent regimes. The number of values in this vector must be equal to the size of the Darcy friction factor vector parameter to calculate tabulated breakpoints.

#### Dependencies

To enable this parameter, set Pressure loss parameterization to ```Tabulated data - Darcy friction factor vs. Reynolds number```.

Darcy friction factor at each breakpoint in the lookup table of Reynolds numbers. The block interpolates between and extrapolates from the breakpoints to obtain the Darcy friction factor at any Reynolds number. Interpolation is handled by the MATLAB `linear` estimator and extrapolation is handled by the `nearest` function.

The Darcy friction factor must not be negative and must align from left to right in order of increasing Reynolds number. The number of values in this vector must be equal to the size of the Reynolds number vector for Darcy friction factor parameter to calculate tabulated breakpoints.

#### Dependencies

To enable this parameter, set Pressure loss parameterization to ```Tabulated data - Darcy friction factor vs. Reynolds number```.

Reynolds number at each breakpoint in the Euler number lookup table. The block interpolates between and extrapolates from the breakpoints to obtain the Reynolds number at any Euler number. Interpolation is handled by the MATLAB `linear` estimator and extrapolation is handled by the `nearest` function.

The Reynolds numbers must be greater than zero and increase monotonically from left to right. They can span across laminar, transient, and turbulent regimes. The number of values in this vector must be equal to the size of the Euler number vector parameter to calculate tabulated breakpoints.

#### Dependencies

To enable this parameter, set Pressure loss parameterization to ```Tabulated data - Euler number vs. Reynolds number```.

Euler number at each breakpoint in the Reynolds number lookup table. The block interpolates between and extrapolates from the breakpoints to obtain the Euler number at any Reynolds number. Interpolation is handled by the MATLAB `linear` estimator and extrapolation is handled by the `nearest` function.

The Euler number must not be negative and must align from left to right in order of increasing Reynolds number. The number of values in this vector must be equal to the size of the Reynolds number vector for Euler number parameter to calculate tabulated breakpoints.

#### Dependencies

To enable this parameter, set Pressure loss parameterization to ```Tabulated data - Euler number vs. Reynolds number```.

Mathematical model for heat transfer between the fluid and the wall. The choice of model determines which expressions to apply and which parameters to specify for heat transfer calculations. See the E-NTU Heat Transfer block for the calculations by parameterization.

Heat transfer coefficient for convection between the fluid and the wall.

#### Dependencies

To enable this parameter, set Heat transfer parameterization to ```Constant heat transfer coefficient```.

Effective surface area used in heat transfer between the fluid and the wall. The effective surface area is the sum of primary and secondary surface areas, the area where the wall is exposed to fluid and the fins, if any are used. Fin surface area is normally scaled by a fin efficiency factor.

Characteristic length for heat transfer between fluid and wall. This length is used to determine the channel hydraulic diameter.

#### Dependencies

To enable this parameter, set Heat transfer parameterization to ```Tabulated data - Colburn factor vs. Reynolds number``` or ```Tabulated data - Nusselt number vs. Reynolds number & Prandtl number```.

Constant value of the Nusselt number for laminar flows. The Nusselt number is required to calculate the heat transfer coefficient between the fluid and the wall. The default value is for cylindrical pipes and tubes.

#### Dependencies

To enable this parameter, set Heat transfer parameterization to ```Correlations for tubes```.

Reynolds number at each breakpoint in the Colburn factor lookup table. The block interpolates between and extrapolates from the breakpoints to obtain the Colburn factor at any Reynolds number. Interpolation is handled by the MATLAB `linear` estimator and extrapolation is handled by the `nearest` function.

The Reynolds numbers must be greater than zero and increase monotonically from left to right. They can span across laminar, transient, and turbulent regimes. The number of values in this vector must be equal to the size of the Colburn factor vector parameter to calculate tabulated breakpoints.

#### Dependencies

To enable this parameter, set Heat transfer parameterization to ```Tabulated data - Colburn factor vs. Reynolds number```.

The Colburn factor at each breakpoint in the Reynolds number lookup table. The block interpolates between and extrapolates from the breakpoints to obtain the Colburn factor at any Reynolds number. Interpolation is handled by the MATLAB `linear` estimator and extrapolation is handled by the `nearest` function.

The Colburn factor must be zero or positive and align from left to right in order of increasing Reynolds number. The number of values in this vector must be equal to the size of the Reynolds number vector for Colburn factor parameter to calculate tabulated breakpoints.

#### Dependencies

To enable this parameter, set Heat transfer parameterization to ```Tabulated data - Colburn factor vs. Reynolds number```.

The Reynolds number at each breakpoint in the Nusselt number lookup table. Either the Reynolds number or the Prandtl number can serve as an independent variable. The block interpolates between and extrapolates from the breakpoints to obtain the Nusselt number at any Reynolds number. Interpolation is handled by the MATLAB `linear` estimator and extrapolation is handled by the `nearest` function.

The Reynolds numbers must be greater than zero and increase monotonically from left to right. They can span across laminar, transient, and turbulent regimes. The size of the vector must equal the number of rows in the Nusselt number table, Nu(Re,Pr) parameter. If the table has m rows and n columns, the Reynolds number vector must be m elements long.

#### Dependencies

To enable this parameter, set Heat transfer parameterization to ```Tabulated data - Nusselt number vs. Reynolds number & Prandtl number```.

Prandtl number at each breakpoint in the Nusselt number lookup table. Either the Prandtl number or the Reynolds number can serve as an independent variable. The block interpolates between and extrapolates from the breakpoints to obtain the Nusselt number at any Prandtl number. Interpolation is handled by the MATLAB `linear` estimator and extrapolation is handled by the `nearest` function.

The Prandlt number must be greater than zero and increase monotonically from left to right. They can span across laminar, transient, and turbulent regimes. The size of the vector must equal the number of columns in the Nusselt number table parameter. If the table has m rows and n columns, the Prandtl number vector must be n elements long.

#### Dependencies

To enable this parameter, set Heat transfer parameterization to ```Tabulated data - Nusselt number vs. Reynolds number & Prandtl number```.

The Nusselt number at each breakpoint in the Reynolds-Prandtl number lookup table. The block interpolates between and extrapolates from the breakpoints to obtain the Nusselt number at any pair of Reynolds and Prandtl numbers. The Nusselt number is required to calculate the heat transfer coefficient.

The Nusselt number must be greater than zero. Each value must align from top to bottom in order of increasing Reynolds number and from left to right in order of increasing Prandtl number. The number of rows must equal the size of the Reynolds number vector for Nusselt number parameter, and the number of columns must equal the size of the Prandtl number vector for Nusselt number parameter.

#### Dependencies

To enable this parameter, set Heat transfer parameterization to ```Tabulated data - Nusselt number vs. Reynolds number & Prandtl number```.

The mass flow rate below which numerical smoothing is applied. This is employed to avoid discontinuity during flow stagnation. See the Simple Heat Exchanger Interface (G) block for more information about these calculations.

Variables Tab

Pressure in the gas channel at the start of simulation.

Temperature in the gas channel at the start of simulation

Density in the gas channel at the start of simulation

## Extended Capabilities

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