# Condenser Evaporator (2P-MA)

Models heat exchange between a moist air network and a network that can undergo phase change

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## Description

The Condenser Evaporator (2P-MA) block models a heat exchanger with one moist air network, which flows between ports A2 and B2, and one two-phase fluid network, which flows between ports A1 and B1. The heat exchanger can act as a condenser or as an evaporator. The fluid streams can be aligned in parallel, counter, or cross-flow configurations.

Example Heat Exchanger for Refrigeration Applications

You can model the moist air side as flow within tubes, flow around the two-phase fluid tubing, or by an empirical, generic parameterization. The moist air side comprises air, trace gas, and water vapor that may condense throughout the heat exchange cycle. The block model accounts for energy transfer from the air to the liquid water condensation layer. This liquid layer does not collect on the heat transfer surface and is assumed to be completely removed from the downstream moist air flow. The moisture condensation rate is returned as a physical signal at port W.

The block uses the Effectiveness-NTU (E-NTU) method to model heat transfer through the shared wall. Fouling on the exchanger walls, which increases thermal resistance and reduces the heat exchange between the two fluids, is also modeled. You can also optionally model fins on both the moist air and two-phase fluid sides. Pressure loss due to viscous friction on both sides of the exchanger can be modeled analytically or by generic parameterization, which you can use to tune to your own data.

You can model the two-phase fluid side as flow within a tube or a set of tubes. The two-phase fluid tubes use a boundary-following model to track the sub-cooled liquid (L), vapor-liquid mixture (M), and super-heated vapor (V) in three zones. The relative amount of space a zone occupies in the system is called a zone length fraction within the system.

Zone Length Fractions in the Two-Phase Fluid Piping

The sum of the zone length fractions in the two-phase fluid tubing equals 1. Port Z returns the zone length fractions as a vector of physical signals for each of the three phases: [L, M, V].

### Heat Exchanger Configuration

The heat exchanger effectiveness is based on the selected heat exchanger configuration, the fluid properties in each phase, the tube geometry and flow configuration on each side of the exchanger, and the usage and size of fins.

Flow Arrangement

The Flow arrangement parameter assigns the relative flow paths between the two sides:

• Parallel flow indicates the fluids are moving in the same direction.

• Counter flow indicates the fluids are moving in parallel, but opposite directions.

• Cross flow indicates the fluids are moving perpendicular to each other.

Thermal Mixing

When Flow arrangement is set to Cross flow, use the Cross flow arrangement parameter to indicate whether the two-phase fluid or moist air flows are separated into multiple paths by baffles or walls. Without these separations, the flow can mix freely and is considered mixed. Both fluids, one fluid, or neither fluid can be mixed in the cross-flow arrangement. Mixing homogenizes the fluid temperature along the direction of flow of the second fluid, and varies perpendicular to the second fluid flow.

Unmixed flows vary in temperature both along and perpendicular to the flow path of the second fluid.

Sample Cross-Flow Configurations

Note that the flow direction during simulation does not impact the selected flow arrangement setting. The ports on the block do not reflect the physical positions of the ports in the physical heat exchange system.

All flow arrangements are single-pass, which means that the fluids do not make multiple turns in the exchanger for additional points of heat transfer. To model a multi-pass heat exchanger, you can arrange multiple Condenser Evaporator (2P-MA) blocks in series or in parallel.

For example, to achieve a two-pass configuration on the two-phase fluid side and a single-pass configuration on the moist air side, you can connect the two-phase fluid sides in series and the moist air sides to the same input in parallel (such as two Mass Flow Rate Source blocks with half of the total mass flow rate), as shown below.

Flow Geometry

The Flow geometry parameter sets the moist air flow arrangement as either inside a tube or set of tubes, or perpendicular to a tube bank. You can also specify an empirical, generic configuration. The two-phase fluid always flows inside a tube or set of tubes.

When Flow geometry is set to Flow perpendicular to bank of circular tubes, use the Tube bank grid arrangement parameter to define the two-phase fluid tube bank alignment as either Inline or Staggered. The red, downward-pointing arrow indicates the direction of moist air flow. Also indicated in the Inline figure are the Number of tube rows along flow direction and the Number of tube segments in each tube row parameters. Here, flow direction refers to the moist air flow, and tube refers to the two-phase fluid tubing. The Length of each tube segment in a tube row parameter is indicated in the Staggered figure.

Fins

The heat exchanger configuration is without fins when the Total fin surface area parameter is set to 0 m^2. Fins introduce additional surface area for additional heat transfer. Each fluid side has a separate fin area.

### Effectiveness-NTU Heat Transfer

The heat transfer rate is calculated for each fluid phase. In accordance with the three fluid zones that occur on the two-phase fluid side of the heat exchanger, the heat transfer rate is calculated in three sections.

The heat transfer in a zone is calculated as:

${Q}_{zone}=ϵ{C}_{\text{Min}}\left({T}_{\text{In,2P}}-{T}_{\text{In,MA}}\right),$

where:

• CMin is the lesser of the heat capacity rates of the two fluids in that zone. The heat capacity rate is the product of the fluid specific heat, cp, and the fluid mass flow rate. CMin is always positive.

• TIn,2P is the zone inlet temperature of the two-phase fluid.

• TIn,MA is the zone inlet temperature of the moist air.

• ε is the heat exchanger effectiveness.

Effectiveness is a function of the heat capacity rate and the number of transfer units, NTU, and also varies based on the heat exchanger flow arrangement, which is discussed in more detail in Effectiveness by Flow Arrangement. The NTU is calculated as:

$NTU=\frac{z}{{C}_{\text{Min}}R},$

where:

• z is the individual zone length fraction.

• R is the total thermal resistance between the two flows, due to convection, conduction, and any fouling on the tube walls:

$R=\frac{1}{{U}_{\text{2P}}{A}_{\text{Th,2P}}}+\frac{{F}_{\text{2P}}}{{A}_{\text{Th,2P}}}+{R}_{\text{W}}+\frac{{F}_{\text{MA}}}{{A}_{\text{Th,MA}}}+\frac{1}{{U}_{\text{MA}}{A}_{\text{Th,MA}}},$

where:

• U is the convective heat transfer coefficient of the respective fluid. This coefficient is discussed in more detail in Two-Phase Fluid Correlations and Moist Air Correlations.

• F is the Fouling factor on the two-phase fluid or moist air side, respectively.

• RW is the Thermal resistance through heat transfer surface.

• ATh is the heat transfer surface area of the respective side of the exchanger. ATh is the sum of the wall surface area, AW, and the Total fin surface area, AF:

${A}_{\text{Th}}={A}_{\text{W}}+{\eta }_{\text{F}}{A}_{\text{F}},$

where ηF is the Fin efficiency.

The total heat transfer rate between the fluids is the sum of the heat transferred in the three zones by the subcooled liquid (QL), liquid-vapor mixture (QM), and superheated vapor (QV):

$Q=\sum {Q}_{\text{Z}}={Q}_{\text{L}}+{Q}_{\text{M}}+{Q}_{\text{V}}.$

Effectiveness by Flow Arrangement

The heat exchanger effectiveness varies according to its flow configuration and the mixing in each fluid. Below are the formulations for effectiveness calculated in the liquid and vapor zones for each configuration. The effectiveness is $\epsilon =1-\mathrm{exp}\left(-NTU\right)$ for all configurations in the mixture zone.

• When Flow arrangement is set to Parallel flow:

$ϵ=\frac{1-\text{exp}\left[-NTU\left(1+{C}_{\text{R}}\right)\right]}{1+{C}_{\text{R}}}$

• When Flow arrangement is set to Counter flow:

$ϵ=\frac{1-\text{exp}\left[-NTU\left(1-{C}_{\text{R}}\right)\right]}{1-{C}_{\text{R}}\text{exp}\left[-NTU\left(1-{C}_{\text{R}}\right)\right]}$

• When Flow arrangement is set to Cross flow and Cross flow arrangement is set to Both fluids unmixed:

$ϵ=1-\text{exp}\left\{\frac{NT{U}^{\text{0}\text{.22}}}{{C}_{\text{R}}}\left[\text{exp}\left(-{C}_{\text{R}}NT{U}^{\text{0}\text{.78}}\right)-1\right]\right\}$

• When Flow arrangement is set to Cross flow and Cross flow arrangement is set to Both fluids mixed:

$ϵ={\left[\frac{1}{1-\text{exp}\left(-NTU\right)}+\frac{{C}_{\text{R}}}{1-\text{exp}\left(-{C}_{\text{R}}NTU\right)}-\frac{1}{NTU}\right]}^{-1}$

When one fluid is mixed and the other unmixed, the equation for effectiveness depends on the relative heat capacity rates of the fluids. When Flow arrangement is set to Cross flow and Cross flow arrangement is set to either Two-Phase Fluid 1 mixed & Moist Air 2 unmixed or Two-Phase Fluid 1 unmixed & Moist Air 2 mixed:

• When the fluid with Cmax is mixed and the fluid with Cmin is unmixed:

$ϵ=\frac{1}{{C}_{\text{R}}}\left(1-\text{exp}\left\{-{C}_{R}\left\{1-\mathrm{exp}\left(-NTU\right)\right\}\right\}\right)$

• When the fluid with Cmin is mixed and the fluid with Cmax is unmixed:

$ϵ=1-\text{exp}\left\{-\frac{1}{{C}_{\text{R}}}\left[1-\text{exp}\left(-{C}_{\text{R}}NTU\right)\right]\right\}$

CR denotes the ratio between the heat capacity rates of the two fluids:

${C}_{\text{R}}=\frac{{C}_{\text{Min}}}{{C}_{\text{Max}}}.$

### Condensation

On the moist air side, a layer of condensation may form on the heat transfer surface. This liquid layer can influence the amount of heat transferred between the moist air and two-phase fluid. The equations for E-NTU heat transfer above are given for dry heat transfer. To correct for the influence of condensation, the E-NTU equations are additionally calculated with the wet parameters listed below. Whichever of the two calculated heat flow rates results in a larger amount of moist air side cooling is used in heat calculations for each zone [1]. To use this method, the Lewis number is assumed to be close to 1 [1], which is true for moist air.

E-NTU Quantities Used for Heat Transfer Rate Calculations

Dry calculationWet calculation
Moist air zone inlet temperatureTin,MATin,wb,MA
Heat capacity rate${\overline{\stackrel{˙}{m}}}_{MA}{\overline{c}}_{p,MA}$${\overline{\stackrel{˙}{m}}}_{MA}{\overline{c}}_{eq,MA}$
Heat transfer coefficientUMA${U}_{MA}\frac{{\overline{c}}_{eq,MA}}{{\overline{c}}_{p,MA}}$

where:

• Tin,MA is the moist air zone inlet temperature.

• Tin,wb,MA is the moist air wet-bulb temperature associated with Tin,MA.

• ${\overline{\stackrel{˙}{m}}}_{MA}$ is the dry air mass flow rate.

• ${\overline{c}}_{p,MA}$ is the moist air heat capacity per unit mass of dry air.

• ${\overline{c}}_{eq,MA}$ is the equivalent heat capacity. The equivalent heat capacity is the change in the moist air specific enthalpy (per unit of dry air), ${\overline{h}}_{MA}$, with respect to temperature at saturated moist air conditions:

${\overline{c}}_{eq,MA}={\left(\frac{\partial {\overline{h}}_{MA}}{\partial {T}_{MA}}\right)}_{s}.$

The mass flow rate of the condensed water vapor leaving the moist air mass flow depends on the relative humidity between the moist air inlet and the channel wall and the heat exchanger NTUs:

${\stackrel{˙}{m}}_{cond}=-{\overline{\stackrel{˙}{m}}}_{MA}\left({W}_{wall,MA}-{W}_{in,MA}\right)\left(1-{e}^{-NT{U}_{MA}}\right),$

where:

• Wwall,MA is the humidity ratio at the heat transfer surface.

• Win,MA is the humidity ratio at the moist air flow inlet.

• NTUMA is the number of transfer units on the moist air side, calculated as:

$NT{U}_{MA}=\frac{{U}_{MA}\frac{{\overline{c}}_{eq,MA}}{{\overline{c}}_{p,MA}}{A}_{Th,MA}}{{\overline{\stackrel{˙}{m}}}_{MA}{\overline{c}}_{eq,MA}}.$

The energy flow associated with water vapor condensation is based on the difference between the vapor specific enthalpy, hwater, wall, and the specific enthalpy of vaporization, hfg, for water:

${\varphi }_{Cond}={\stackrel{˙}{m}}_{cond}\left({h}_{water,wall}-{h}_{fg}\right).$

The condensate is assumed to not accumulate on the heat transfer surface, and does not influence geometric parameters such as tube diameter. The condensed water is assumed to be completely removed from the downstream moist air flow.

### Two-Phase Fluid Correlations

Heat Transfer Coefficient

The convective heat transfer coefficient varies according to the fluid Nusselt number:

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

where:

• Nu is the zone mean Nusselt number, which depends on the flow regime.

• k is the fluid phase thermal conductivity.

• DH is tube hydraulic diameter.

For turbulent flows in the subcooled liquid or superheated vapor zones, the Nusselt number is calculated with the Gnielinski correlation:

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

where:

• Re is the fluid Reynolds number.

• Pr is the fluid Prandtl number.

For turbulent flows in the liquid-vapor mixture zone, the Nusselt number is calculated with the Cavallini-Zecchin correlation:

$\text{Nu}=\frac{{\text{aRe}}_{\text{SL}}^{b}{\text{Pr}}_{\text{SL}}^{c}\left\{{\left[\left(\sqrt{\frac{{\rho }_{\text{SL}}}{{\rho }_{\text{SV}}}}-1\right){x}_{\text{Out}}+1\right]}^{1+b}-{\left[\left(\sqrt{\frac{{\rho }_{\text{SL}}}{{\rho }_{\text{SV}}}}-1\right){x}_{\text{In}}+1\right]}^{1+b}\right\}}{\left(1+b\right)\left(\sqrt{\frac{{\rho }_{\text{SL}}}{{\rho }_{\text{SV}}}}-1\right)\left({x}_{\text{Out}}-{x}_{\text{In}}\right)}.$

where:

• ReSL is the Reynolds number of the saturated liquid.

• PrSL is the Prandtl number of the saturated liquid.

• ρSL is the density of the saturated liquid.

• ρSV is the density of the saturated vapor.

• a= 0.05, b = 0.8, and c= 0.33.

For laminar flows, the Nusselt number is set by the Laminar flow Nusselt number parameter.

For transitional flows, the Nusselt number is a blend between the laminar and turbulent Nusselt numbers.

Empirical Nusselt Number Formulation

When the Heat transfer coefficient model parameter is set to Colburn equation, the Nusselt number for the subcooled liquid and superheated vapor zones is calculated by the empirical the Colburn equation:

$\text{Nu}=a{\text{Re}}^{b}{\text{Pr}}^{c},$

where a, b, and c are defined in the Coefficients [a, b, c] for a*Re^b*Pr^c in liquid zone and Coefficients [a, b, c] for a*Re^b*Pr^c in vapor zone parameters.

The Nusselt number for liquid-vapor mixture zones is calculated with the Cavallini-Zecchin equation, with the variables specified in the Coefficients [a, b, c] for a*Re^b*Pr^c in mixture zone parameter.

Pressure Loss

The pressure loss due to viscous friction varies depending on flow regime and configuration. The calculation uses the overall density, which is the total two-phase fluid mass divided by the total two-phase fluid volume.

For turbulent flows, when the Reynolds number is above the Turbulent flow lower Reynolds number limit, the pressure loss due to friction is calculated in terms of the Darcy friction factor. The pressure differential between port A1 and the internal node I1 is:

${p}_{\text{A1}}-{p}_{\text{I1}}=\frac{{f}_{\text{D,A}}{\stackrel{˙}{m}}_{\text{A1}}|{\stackrel{˙}{m}}_{\text{A1}}|}{2\rho {D}_{\text{H}}{A}_{\text{CS}}^{2}}\left(\frac{L+{L}_{\text{Add}}}{2}\right),$

where:

• $\stackrel{˙}{m}$A1 is the total flow rate through port A1.

• fD,A is the Darcy friction factor, according to the Haaland correlation:

${f}_{\text{D,A1}}={\left\{-1.8{\text{log}}_{\text{10}}\left[\frac{6.9}{{\text{Re}}_{\text{A1}}}+{\left(\frac{{ϵ}_{\text{R}}}{3.7{D}_{\text{H}}}\right)}^{1.11}\right]\right\}}^{\text{-2}},$

where εR is the two-phase fluid pipe Internal surface absolute roughness. Note that the friction factor is dependent on the Reynolds number, and is calculated at both ports for each liquid.

• L is the Total length of each tube on the two-phase fluid side.

• LAdd is the two-phase fluid side Aggregate equivalent length of local resistances, which is the equivalent length of a tube that introduces the same amount of loss as the sum of the losses due to other local resistances in the tube.

• ACS is the tube cross-sectional area.

The pressure differential between port B1 and internal node I1 is:

${p}_{\text{B1}}-{p}_{\text{I1}}=\frac{{f}_{\text{D,B}}{\stackrel{˙}{m}}_{\text{B1}}|{\stackrel{˙}{m}}_{\text{B1}}|}{2\rho {D}_{\text{H}}{A}_{\text{CS}}^{2}}\left(\frac{L+{L}_{\text{Add}}}{2}\right),$

where $\stackrel{˙}{m}$B1 is the total flow rate through port B1.

The Darcy friction factor at port B1 is:

${f}_{\text{D,B1}}={\left\{-1.8{\text{log}}_{\text{10}}\left[\frac{6.9}{{\text{Re}}_{\text{B1}}}+{\left(\frac{{ϵ}_{\text{R}}}{3.7{D}_{\text{H}}}\right)}^{1.11}\right]\right\}}^{\text{-2}}.$

For laminar flows, when the Reynolds number is below the Laminar flow upper Reynolds number limit, the pressure loss due to friction is calculated in terms of the Laminar friction constant for Darcy friction factor, λ. λ is a user-defined parameter when Tube cross-section is set to Generic, otherwise, the value is calculated internally. The pressure differential between port A1 and internal node I1 is:

${p}_{\text{A1}}-{p}_{\text{I1}}=\frac{\lambda \mu {\stackrel{˙}{m}}_{\text{A1}}}{2\rho {D}_{\text{H}}^{2}{A}_{CS}}\left(\frac{L+{L}_{\text{Add}}}{2}\right),$

where μ is the two-phase fluid dynamic viscosity. The pressure differential between port B1 and internal node I1 is:

${p}_{\text{B1}}-{p}_{\text{I1}}=\frac{\lambda \mu {\stackrel{˙}{m}}_{\text{B1}}}{2\rho {D}_{\text{H}}^{2}{A}_{CS}}\left(\frac{L+{L}_{\text{Add}}}{2}\right).$

For transitional flows, the pressure differential due to viscous friction is a smoothed blend between the values for laminar and turbulent pressure losses.

Empirical Pressure Loss Formulation

When Pressure loss model is set to Pressure loss coefficient, the pressure losses due to viscous friction are calculated with an empirical pressure loss coefficient, ξ.

The pressure differential between port A1 and internal node I1 is:

${p}_{\text{A1}}-{p}_{\text{I1}}=\frac{1}{2}\xi \frac{{\stackrel{˙}{m}}_{\text{A1}}|{\stackrel{˙}{m}}_{\text{A1}}|}{2\rho {A}_{\text{CS}}^{2}}.$

The pressure differential between port B1 and internal node I1 is:

${p}_{\text{B1}}-{p}_{\text{I1}}=\frac{1}{2}\xi \frac{{\stackrel{˙}{m}}_{\text{B1}}|{\stackrel{˙}{m}}_{\text{B1}}|}{2\rho {A}_{\text{CS}}^{2}}.$

### Moist Air Correlations

Heat Transfer Coefficient for Flows Inside One or More Tubes

When the moist air Flow geometry is set to Flow inside one or more tubes, the Nusselt number is calculated according to the Gnielinski correlation in the same manner as two-phase supercooled liquid or superheated vapor. See Heat Transfer Coefficient for more information.

Heat Transfer Coefficient for Flows Across a Tube Bank

When the moist air Flow geometry is set to Flow perpendicular to bank of circular tubes, the Nusselt number is calculated based on the Hagen number, Hg, and depends on the Tube bank grid arrangement setting:

$\text{Nu}=\left\{\begin{array}{cc}0.404L{q}^{\text{1/3}}{\left(\frac{\text{Re}+1}{\text{Re}+1000}\right)}^{0.1},& Inline\\ 0.404L{q}^{1/3},& Staggered\end{array}$

where:

$Lq=\left\{\begin{array}{cc}1.18\text{Pr}\left(\frac{4{l}_{\text{T}}/\pi -D}{{l}_{\text{L}}}\right)\text{Hg}\left(\text{Re}\right),& Inline\\ 0.92\text{Pr}\left(\frac{4{l}_{\text{T}}/\pi -D}{{l}_{\text{D}}}\right)\text{Hg}\left(\text{Re}\right),& Staggeredwith{l}_{L}\ge D\\ 0.92\text{Pr}\left(\frac{4{l}_{\text{T}}{l}_{\text{L}}/\pi -{D}^{2}}{{l}_{\text{L}}{l}_{\text{D}}}\right)\text{Hg}\left(\text{Re}\right),& Staggeredwith{l}_{L}

• D is the Tube outer diameter.

• lL is the Longitudinal tube pitch (along flow direction), the distance between the tube centers along the flow direction. Flow direction refers to the moist air flow.

• lT is the Transverse tube pitch (perpendicular to flow direction), shown in the figure below. The transverse pitch is the distance between the centers of the two-phase fluid tubing in one row.

• lD is the diagonal tube spacing, calculated as ${l}_{\text{D}}=\sqrt{{\left(\frac{{l}_{\text{T}}}{2}\right)}^{2}+{l}_{\text{L}}^{2}}.$

For more information on calculating the Hagen number, see [6].

The longitudinal and transverse pitch distances are the same for both grid bank arrangement types.

Cross-Section of Two-Phase Fluid Tubing with Pitch Measurements

Empirical Nusselt Number Forumulation

When the Heat transfer coefficient model is set to Colburn equation or when Flow geometry is set to Generic, the Nusselt number is calculated by the empirical the Colburn equation:

$\text{Nu}=a{\text{Re}}^{b}{\text{Pr}}^{c},$

where a, b, and c are the values defined in the Coefficients [a, b, c] for a*Re^b*Pr^c parameter.

Pressure Loss for Flow Inside Tubes

When the moist air Flow geometry is set to Flow inside one or more tubes, the pressure loss is calculated in the same manner as for two-phase flows, with the respective Darcy friction factor, density, mass flow rates, and pipe lengths of the moist air side. See Pressure Loss for more information.

Pressure Loss for Flow Across Tube Banks

When the moist air Flow geometry is set to Flow perpendicular to bank of circular tubes, the Hagen number is used to calculate the pressure loss due to viscous friction. The pressure differential between port A2 and internal node I2 is:

${p}_{\text{A2}}-{p}_{\text{I2}}=\frac{1}{2}\frac{{\mu }^{2}{N}_{\text{R}}}{\rho {D}^{2}}\text{Hg}\left(\text{Re}\right),$

where:

• μMA is the fluid dynamic viscosity.

• NR is the Number of tube rows along flow direction. This is the number of two-phase fluid tube rows along the moist air flow direction.

The pressure differential between port B2 and internal node I2 is:

${p}_{\text{B2}}-{p}_{\text{I2}}=\frac{1}{2}\frac{{\mu }^{2}{N}_{\text{R}}}{\rho {D}^{2}}\text{Hg}\left(\text{Re}\right).$

Empirical Pressure Loss Formulation

When the Pressure loss model is set to Euler number per tube row or when Flow geometry is set to Generic, the pressure loss due to viscous friction is calculated with a pressure loss coefficient, in terms of the Euler number, Eu:

$\text{Eu}=\frac{\xi }{{N}_{R}},$

where ξ is the empirical pressure loss coefficient.

The pressure differential between port A2 and internal node I2 is:

${p}_{\text{A2}}-{p}_{\text{I2}}=\frac{1}{2}{N}_{R}Eu\frac{{\stackrel{˙}{m}}_{\text{A2}}|{\stackrel{˙}{m}}_{\text{A2}}|}{2\rho {A}_{\text{CS}}^{2}}.$

The pressure differential between port B2 and internal node I2 is:

${p}_{\text{B2}}-{p}_{\text{I2}}=\frac{1}{2}{N}_{R}Eu\frac{{\stackrel{˙}{m}}_{\text{B2}}|{\stackrel{˙}{m}}_{\text{B2}}|}{2\rho {A}_{\text{CS}}^{2}}.$

### Conservation Equations

Two-Phase Fluid

The total mass accumulation rate in the two-phase fluid is defined as:

$\frac{d{M}_{\text{2P}}}{dt}={\stackrel{˙}{m}}_{\text{A1}}+{\stackrel{˙}{m}}_{\text{B1}},$

where:

• M2P is the total mass of the two-phase fluid.

• $\stackrel{˙}{m}$A1 is the mass flow rate of the fluid at port A1.

• $\stackrel{˙}{m}$B1 is the mass flow rate of the fluid at port B1.

The flow is positive when flowing into the block through the port.

The energy conservation equation relates the change in specific internal energy to the heat transfer by the fluid:

${M}_{2P}\frac{d{u}_{2P}}{dt}+{u}_{2P}\left({\stackrel{˙}{m}}_{A1}+{\stackrel{˙}{m}}_{B1}\right)={\varphi }_{\text{A1}}+{\varphi }_{\text{B1}}-Q,$

where:

• u2P is the two-phase fluid specific internal energy.

• φA1 is the energy flow rate at port A1.

• φB1 is the energy flow rate at port B1.

• Q is heat transfer rate, which is positive when leaving the two-phase fluid volume.

Moist Air

There are three equations for mass conservation on the moist air side: one for the moist air mixture, one for condensed water vapor, and one for the trace gas.

Note

If Trace gas model is set to None in the Moist Air Properties (MA) block, the trace gas is not modeled in blocks in the moist air network. In the Condenser Evaporator (2P-MA) block, this means that the conservation equation for trace gas is set to 0.

The moist air mixture mass accumulation rate accounts for the changes of the entire moist air mass flow through the exchanger ports and the condensation mass flow rate:

$\frac{d{M}_{\text{MA}}}{dt}={\stackrel{˙}{m}}_{\text{A2}}+{\stackrel{˙}{m}}_{\text{B2}}-{\stackrel{˙}{m}}_{\text{Cond}}.$

The mass conservation equation for water vapor accounts for the water vapor transit through the moist air side and condensation formation:

$\frac{d{x}_{w}}{dt}{M}_{\text{MA}}+{x}_{\text{w}}\left({\stackrel{˙}{m}}_{\text{A2}}+{\stackrel{˙}{m}}_{\text{B2}}-{\stackrel{˙}{m}}_{\text{Cond}}\right)={\stackrel{˙}{m}}_{\text{w,A2}}+{\stackrel{˙}{m}}_{\text{w,B2}}-{\stackrel{˙}{m}}_{\text{Cond}},$

where:

• xw is the mass fraction of the vapor. $\frac{d{x}_{w}}{dt}$ is the rate of change of this fraction.

• ${\stackrel{˙}{m}}_{\text{w,A2}}$ is the water vapor mass flow rate at port A2.

• ${\stackrel{˙}{m}}_{\text{w,B2}}$ is the water vapor mass flow rate at port B2.

• ${\stackrel{˙}{m}}_{Cond}$ is the rate of condensation.

The trace gas mass balance is:

$\frac{d{x}_{\text{g}}}{dt}{M}_{\text{MA}}+{x}_{\text{g}}\left({\stackrel{˙}{m}}_{\text{A2}}+{\stackrel{˙}{m}}_{\text{B2}}-{\stackrel{˙}{m}}_{\text{Cond}}\right)={\stackrel{˙}{m}}_{\text{g,A2}}+{\stackrel{˙}{m}}_{\text{g,B2}},$

where:

• xg is the mass fraction of the trace gas. $\frac{d{x}_{g}}{dt}$ is the rate of change of this fraction.

• ${\stackrel{˙}{m}}_{\text{g,A2}}$ is the trace gas mass flow rate at port A2.

• ${\stackrel{˙}{m}}_{\text{g,B2}}$ is the trace gas mass flow rate at port B2.

Energy conservation on the moist air side accounts for the change in specific internal energy due to heat transfer and water vapor condensing out of the moist air mass:

${M}_{MA}\frac{d{u}_{MA}}{dt}+{u}_{MA}\left({\stackrel{˙}{m}}_{A2}+{\stackrel{˙}{m}}_{B2}-{\stackrel{˙}{m}}_{Cond}\right)={\varphi }_{\text{A2}}+{\varphi }_{\text{B2}}+Q-{\varphi }_{\text{Cond}},$

where:

• ϕA2 is the energy flow rate at port A2.

• ϕB2 is the energy flow rate at port B2.

• ϕCond is the energy flow rate due to condensation.

The heat transferred to or from the moist air, Q, is equal to the heat transferred from or to the two-phase fluid.

## Ports

### Conserving

expand all

Inlet or outlet port associated with the two-phase fluid.

Inlet or outlet port associated with the two-phase fluid.

Inlet or outlet port associated with the moist air.

Inlet or outlet port associated with the moist air.

### Output

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Three-element vector of the zone length fractions in the two-phase fluid channel, returned as a physical signal. The vector takes the form [L, M, V], where L is the sub-cooled liquid, M is the liquid-vapor mixture, and V is the superheated vapor.

Water condensation rate in the moist air flow, returned as a physical signal. The condensate does not accumulate on the heat transfer surface.

## Parameters

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### Configuration

Flow path alignment between the heat exchanger sides. The available flow arrangements are:

• Parallel flow. The flows run in the same direction.

• Counter flow. The flows run parallel to each other, in the opposite directions.

• Cross flow. The flows run perpendicular to each other.

Select whether each of the fluids can mix in its channel. Mixed flow means that the fluid is free to move in the transverse direction as it travels along the flow path. Unmixed flow means that the fluid is restricted to travel only along the flow path. For example, a side with fins is considered an unmixed flow.

#### Dependencies

To enable this parameter, set Flow arrangement to Cross flow.

Thermal resistance of the wall that separates the two sides of the heat exchanger. The wall thermal resistance, wall fouling, and fluid convective heat transfer coefficient influence the amount of heat transferred between the flows.

Flow area at the two-phase fluid port A1.

Flow area at the two-phase fluid port B1.

Flow area at the moist air side port A2.

Flow area at the moist air side port B2.

### Two-Phase Fluid 1

Number of two-phase fluid tubes.

Total length of each two-phase fluid tube.

Cross-sectional shape of a tube. Use Generic to specify an arbitrary cross-sectional geometry.

This parameter specifies the cross-section of one tube.

Internal diameter of the cross-section of one tube. The cross-section and diameter are uniform along the tube. The size of the diameter influences the pressure loss and heat transfer calculations.

#### Dependencies

To enable this parameter, set Tube cross-section to Circular.

Internal width of the cross-section of one tube. The cross-section and width are uniform along the tube. The width and height influence the pressure loss and heat transfer calculations.

#### Dependencies

To enable this parameter, set Tube cross-section to Rectangular.

Internal height of one tube. The cross-section and height are uniform along the tube. The width and height influence the pressure loss and heat transfer calculations.

#### Dependencies

To enable this parameter, set Tube cross-section to Rectangular.

Smaller diameter of the annular cross-section of one tube. The cross-section and inner diameter are uniform along the tube. The inner diameter influences the pressure loss and heat transfer calculations. Heat transfer occurs through the inner surface of the annulus.

#### Dependencies

To enable this parameter, set Tube cross-section to Annular.

Larger diameter of the annular cross-section of one tube. The cross-section and outer diameter are uniform along the tube. The outer diameter influences the pressure loss and heat transfer calculations.

#### Dependencies

To enable this parameter, set Tube cross-section to Annular.

Internal flow area of each tube.

#### Dependencies

To enable this parameter, set Tube cross-section to Generic.

Perimeter of the tube cross-section that the fluid touches. The cross-section and perimeter are uniform along the tube. This value is applied in pressure loss calculations.

#### Dependencies

To enable this parameter, set Tube cross-section to Generic.

Tube perimeter for heat transfer calculations. This is often the same as the tube perimeter, but in cases such as the annular cross-section, this may be only the inner or outer diameter, depending on the heat-transferring surface. The cross-section and tube perimeter are uniform along the tube.

#### Dependencies

To enable this parameter, set Tube cross-section to Generic.

Method of pressure loss calculation due to viscous friction. The settings are:

• Pressure loss coefficient. Use this setting to calculate the pressure loss based on an empirical loss coefficient.

• Correlation for flow inside tubes. Use this setting to calculate the pressure loss based on the pipe flow correlation.

Empirical loss coefficient for all pressure losses in the channel. This value accounts for wall friction and minor losses due to bends, elbows, and other geometry changes in the channel.

The loss coefficient can be calculated from a nominal operating condition or be tuned to fit experimental data. The loss coefficient is defined as:

$\xi =\frac{\Delta p}{\frac{1}{2}\rho {v}^{2}},$

where Δp is the pressure drop, ρ is the two-phase fluid density, and v is the flow velocity.

#### Dependencies

To enable this parameter, set Pressure loss model to Pressure loss coefficient.

Combined length of all local resistances in the tubes. This parameter describes the length of tubing that results in the same pressure losses as the sum of all minor losses in the tube due to bends, tees, or unions. A longer equivalent length results in larger pressure losses.

#### Dependencies

To enable this parameter, set Pressure loss model to Correlation for flow inside tubes.

Mean height of tube surface defects. A rougher wall results in larger pressure losses in the turbulent regime for pressure loss calculated with the Haaland correlation.

#### Dependencies

To enable this parameter, set either:

• Pressure loss model

• Heat transfer model

to Correlation for flow inside tubes.

Largest Reynolds number that indicates laminar flow. Between this value and the Turbulent flow lower Reynolds number, the flow regime is transitional.

Smallest Reynolds number that indicates turbulent flow. Between this value and the Laminar flow upper Reynolds number limit, the flow regime is transitional.

Coefficient in pressure loss equations for viscous friction in laminar flows. This parameter may also be known as the shape factor. The default value corresponds to a circular tube cross-section.

#### Dependencies

To enable this parameter, set Tube cross section to Generic and Pressure loss model to Correlation for flow inside tubes.

Method of calculating the heat transfer coefficient between the fluid and the wall. The available settings are:

• Colburn equation. Use this setting to calculate the heat transfer coefficient with user-defined variables a, b, and c. In the liquid and vapor zones, the heat transfer coefficient is based on the Colburn equation. In the liquid-vapor mixture zone, the heat transfer coefficient is based on the Cavallini-Zecchin equation.

• Correlation for flow inside tubes. Use this setting to calculate the heat transfer coefficient for pipe flows. In the liquid and vapor zones, the heat transfer coefficient is calculated with the Gnielinski correlation. In the liquid-vapor mixture zone, the heat transfer coefficient is calculated with the Cavallini-Zecchin equation.

Three-element vector containing the empirical coefficients of the Colburn equation. Each fluid zone has a distinct Nusselt number, which is calculated by the Colburn equation per zone. The general form of the Colburn equation is:

$\text{Nu}=a{\text{Re}}^{b}{\text{Pr}}^{c}.$

#### Dependencies

To enable this parameter, set Heat transfer coefficient model to Colburn equation.

Three-element vector containing the empirical coefficients of the Cavallini-Zecchin equation. Each fluid zone has a distinct Nusselt number, which is calculated in the mixture zone by the Cavallini-Zecchin equation:

$\text{Nu}=\frac{{\text{aRe}}_{\text{SL}}^{b}{\text{Pr}}_{\text{SL}}^{c}\left\{{\left[\left(\sqrt{\frac{{\rho }_{\text{SL}}}{{\rho }_{\text{SV}}}}-1\right){x}_{\text{Out}}+1\right]}^{1+b}-{\left[\left(\sqrt{\frac{{\rho }_{\text{SL}}}{{\rho }_{\text{SV}}}}-1\right){x}_{\text{In}}+1\right]}^{1+b}\right\}}{\left(1+b\right)\left(\sqrt{\frac{{\rho }_{\text{SL}}}{{\rho }_{\text{SV}}}}-1\right)\left({x}_{\text{Out}}-{x}_{\text{In}}\right)}.$

#### Dependencies

To enable this parameter, set Heat transfer coefficient model to Colburn equation.

Three-element vector containing the empirical coefficients of the Colburn equation. Each fluid zone has a distinct Nusselt number, which is calculated by the Colburn equation per zone. The general form of the Colburn equation is:

$\text{Nu}=a{\text{Re}}^{b}{\text{Pr}}^{c}.$

#### Dependencies

To enable this parameter, set Heat transfer coefficient model to Colburn equation.

Ratio of convective to conductive heat transfer in the laminar flow regime. The fluid Nusselt number influences the heat transfer rate and depends on the tube cross-section.

#### Dependencies

To enable this parameter, set Heat transfer coefficient model to Correlation for flow inside tubes.

Additional thermal resistance due to fouling layers on the surfaces of the wall. In real systems, fouling deposits grow over time. However, the growth is slow enough to be assumed constant during the simulation.

Total heat transfer surface area of both sides of all fins. For example, if the fin is rectangular, the surface area is double the area of the rectangle.

The total heat transfer surface area is the sum of the channel surface area and the effective fin surface area, which is the product of the Fin efficiency and the Total fin surface area.

Ratio of actual heat transfer to ideal heat transfer through the fins.

Quantity used to describe the initial state of the fluid: temperature, vapor quality, vapor void fraction, specific enthalpy, or specific internal energy.

Fluid pressure at the start of the simulation.

Temperature in the two-phase fluid channel at the start of simulation. This parameter can be a scalar or a two-element vector. A scalar value represents the mean initial temperature in the channel. A vector value represents the initial temperature at the inlet and outlet in the form [inlet, outlet]. The block calculates a linear gradient between the two ports. The inlet and the outlet ports are identified according to the initial flow direction.

#### Dependencies

To enable this parameter, set Initial fluid energy specification to Temperature.

Vapor mass fraction in the two-phase fluid channel at the start of simulation. This parameter can be a scalar or a two-element vector. A scalar value represents the mean initial vapor quality in the channel. A vector value represents the initial vapor quality at the inlet and outlet in the form [inlet, outlet]]. The block calculates a linear gradient between the two ports. The inlet and the outlet ports are identified according to the initial flow direction.

#### Dependencies

To enable this parameter, set Initial fluid energy specification to Vapor quality.

Vapor volume fraction in the two-phase fluid channel at the start of simulation. This parameter can be a scalar or a two-element vector. A scalar value represents the mean initial void fraction in the channel. A vector value represents the initial void fraction at the inlet and outlet in the form [inlet, outlet]. The block calculates a linear gradient between the two ports. The inlet and the outlet ports are identified according to the initial flow direction.

#### Dependencies

To enable this parameter, set Initial fluid energy specification to Vapor void fraction.

Enthalpy per unit mass in the two-phase fluid channel at the start of simulation. This parameter can be a scalar or a two-element vector. A scalar value represents the mean initial specific enthalpy in the channel. A vector value represents the initial specific enthalpy at the inlet and outlet in the form [inlet, outlet]. The block calculates a linear gradient between the two ports. The inlet and the outlet ports are identified according to the initial flow direction.

#### Dependencies

To enable this parameter, set Initial fluid energy specification to Specific enthalpy.

Internal energy per unit mass in the two-phase fluid channel at the start of simulation. This parameter can be a scalar or a two-element vector. A scalar value represents the mean initial specific internal energy in the channel. A vector value represents the initial specific internal energy at the inlet and outlet in the form [inlet, outlet]. The block calculates a linear gradient between the two ports. The inlet and the outlet ports are identified according to the initial flow direction.

#### Dependencies

To enable this parameter, set Initial fluid energy specification to Specific internal energy.

### Moist Air 2

Moist air flow path. The flow can run externally over a set of tubes or internal to a tube or set of tubes. You can also specify a generic parameterization based on empirical values.

Number of moist air tubes. More tubes result in higher pressure losses due to viscous friction, but a larger amount of surface area for heat transfer.

#### Dependencies

To enable this parameter, set Flow geometry to Flow inside one or more tubes.

Total length of each moist air tube.

#### Dependencies

To enable this parameter, set Flow geometry to Flow inside one or more tubes.

Cross-sectional shape of one tube. Set to Generic to specify an arbitrary cross-sectional geometry.

#### Dependencies

To enable this parameter, set Flow geometry to Flow inside one or more tubes.

Internal diameter of the cross-section of one tube. The cross-section and diameter are uniform along the tube. The size of the diameter influences the pressure loss and heat transfer calculations.

#### Dependencies

To enable this parameter, set Flow geometry to Flow inside one or more tubes and Tube cross-section to Circular.

Internal width of the cross-section of one tube. The cross-section and width are uniform along the tube. The width and height influence the pressure loss and heat transfer calculations.

#### Dependencies

To enable this parameter, set Flow geometry to Flow inside one or more tubes and Tube cross-section to Rectangular.

Internal height of one tube cross-section. The cross-section and height are uniform along the tube. The width and height influence the pressure loss and heat transfer calculations.

#### Dependencies

To enable this parameter, set Flow geometry parameterization of Flow inside one or more tubes and Tube cross-section to Rectangular.

Smaller diameter of the annular cross-section of one tube. The cross-section and inner diameter are uniform along the tube. The inner diameter influences the pressure loss and heat transfer calculations. Heat transfer occurs through the inner surface of the annulus.

#### Dependencies

To enable this parameter, set Flow geometry parameterization of Flow inside one or more tubes and Tube cross-section to Annular.

Larger diameter of the annular cross-section of one tube. The cross-section and outer diameter are uniform along the tube. The outer diameter influences the pressure loss and heat transfer calculations.

#### Dependencies

To enable this parameter, set Flow geometry to Flow inside one or more tubes and Tube cross-section to Annular.

Internal flow area of each tube.

#### Dependencies

To enable this parameter, set Flow geometry to Flow inside one or more tubes and Tube cross-section to Generic.

Perimeter of the tube cross-section that the fluid touches. The cross-section and perimeter are uniform along the tube. This value is applied in pressure loss calculations.

#### Dependencies

To enable this parameter, set Flow geometry to Flow inside one or more tubes and Tube cross-section to Generic.

Tube perimeter for heat transfer calculations. This is often the same as the tube perimeter, but in cases such as the annular cross-section, this may be only the inner or outer diameter, depending on the heat-transferring surface. The cross-section and tube perimeter are uniform along the tube.

#### Dependencies

To enable this parameter, set Flow geometry to Flow inside one or more tubes and Tube cross-section to Generic.

Method of pressure loss calculation due to viscous friction. Different models are available for different flow configurations. The settings are:

• Correlation for flow inside tubes. Use this setting to calculate the pressure loss with the Haaland correlation.

• Pressure loss coefficient. Use this setting to calculate the pressure loss based on an empirical loss coefficient.

• Euler number per tube row. Use this setting to calculate the pressure loss based on an empirical Euler number.

• Correlation for flow over tube bank. Use this setting to calculate the pressure loss based on the Hagen number.

The pressure loss models available depend on the Flow geometry setting.

#### Dependencies

When Flow geometry is set to Flow inside one or more tubes, Pressure loss model can be set to either:

• Pressure loss coefficient.

• Correlation for flow inside tubes.

When Flow geometry is set to Flow perpendicular to bank of circular tubes, Pressure loss model can be set to either:

• Correlation for flow over tube bank.

• Euler number per tube row.

When Flow geometry is set to Generic, the Pressure loss model parameter is disabled. Pressure loss is calculated empirically with the Pressure loss coefficient, delta_p/(0.5*rho*v^2) parameter.

Empirical loss coefficient for all pressure losses in the channel. This value accounts for wall friction and minor losses due to bends, elbows, and other geometry changes in the channel.

The loss coefficient can be calculated from a nominal operating condition or be tuned to fit experimental data. The pressure loss coefficient is defined as:

$\xi =\frac{\Delta p}{\frac{1}{2}\rho {v}^{2}},$

where Δp is the pressure drop, ρ is the two-phase fluid density, and v is the flow velocity.

#### Dependencies

To enable this parameter, set either:

• Flow geometry to Generic.

• Pressure loss model to Pressure loss coefficient.

Combined length of all local resistances in the tubes. This is the length of tubing that results in the same pressure losses as the sum of all minor losses in the tube due to such things as bends, tees, or unions. A longer equivalent length results in larger pressure losses.

#### Dependencies

To enable this parameter, set Pressure loss model to Correlations for flow inside tubes.

Mean height of tube surface defects. A rougher wall results in larger pressure losses in the turbulent regime for pressure loss calculated with the Haaland correlation.

#### Dependencies

To enable this parameter, set either:

• Pressure loss model

• Heat transfer coefficient model

to Correlation for flow inside tubes.

Largest Reynolds number that indicates laminar flow. Between this value and the Turbulent flow lower Reynolds number limit, the flow regime is transitional.

#### Dependencies

To enable this parameter, set Flow geometry to Flow inside one or more tubes and Pressure loss model to Correlation for flow inside tubes.

Smallest Reynolds number that indicates turbulent flow. Between this value and the Laminar flow upper Reynolds number limit, the flow regime is transitional between the laminar and turbulent regimes.

#### Dependencies

To enable this parameter, set Flow geometry to Flow inside one or more tubes and Pressure loss model to Correlation for flow inside tubes.

Coefficient in pressure loss equations for viscous friction in laminar flows. This parameter is also known as the shape factor. The default value corresponds to a circular tube cross-section.

#### Dependencies

To enable this parameter, set Flow geometry to Correlation for flow inside tubes, Tube cross section to Generic, and Pressure loss model to Correlation for flow inside tubes.

Method of calculating the heat transfer coefficient between the fluid and the wall. The available settings are:

• Colburn equation. Use this setting to calculate the heat transfer coefficient with user-defined variables a, b, and c of the Colburn equation.

• Correlation for flow over tube bank. Use this setting to calculate the heat transfer coefficient based on the tube bank correlation using the Hagen number.

• Correlation for flow inside tubes. Use this setting to calculate the heat transfer coefficient for pipe flows with the Gnielinski correlation.

#### Dependencies

To enable this parameter, set Flow geometry to either:

• Flow perpendicular to bank of circular tubes.

• Flow inside one or more tubes.

Three-element vector containing the empirical coefficients of the Colburn equation. The Colburn equation is a formulation for calculating the Nusselt Number. The general form of the Colburn equation is:

$\text{Nu}=a{\text{Re}}^{b}{\text{Pr}}^{c}.$

When the Heat transfer coefficient model is set to Colburn equation and Flow geometry is set to Flow inside one or more tubes, or Flow geometry is set to Generic, the default Colburn equation is:

$\text{Nu}=0.023{\text{Re}}^{0.8}{\text{Pr}}^{1/3}.$

When the Heat transfer coefficient model is set to Colburn equation and Flow geometry is set to Flow perpendicular to bank of circular tubes, the default Colburn equation is:

$\text{Nu}=0.27{\text{Re}}^{0.63}{\text{Pr}}^{0.36}.$

#### Dependencies

To enable this parameter, set:

1. Flow geometry to either:

• Flow inside one or more tubes

• Flow perpendicular to bank of circular tubes

and Heat transfer coefficient model to Colburn equation.

2. Flow geometry to Generic.

Ratio of convective to conductive heat transfer in the laminar flow regime. The fluid Nusselt number influences the heat transfer rate and depends on the tube cross-section.

#### Dependencies

To enable this parameter, set Flow geometry to Flow inside one or more tubes, Tube cross-section to Generic, and Heat transfer parameterization to Correlation for flow inside tubes.

Alignment of tubes in a tube bank. Rows are either in line with their neighbors, or staggered.

• Inline: All tube rows are located directly behind each other.

• Staggered: Tubes of the one tube row are located at the gap between tubes of the previous tube row.

Tube alignment influences the Nusselt number and the heat transfer rate.

#### Dependencies

To enable this parameter, set Flow geometry to Flow perpendicular to bank of circular tubes.

Number of two-phase fluid tube rows in a tube bank. The rows are aligned with the direction of moist air flow.

#### Dependencies

To enable this parameter, set Flow geometry to Flow perpendicular to bank of circular tubes.

Number of two-phase fluid tubes in each row of a tube bank. This measurement is perpendicular to the moist air flow.

#### Dependencies

To enable this parameter, set Flow geometry to Flow perpendicular to bank of circular tubes.

Length of each two-phase fluid tube that spans a tube row. All tubes in a tube bank are the same length.

#### Dependencies

To enable this parameter, set Flow geometry to Flow perpendicular to bank of circular tubes.

Outer diameter of a two-phase fluid tube. The cross-section is uniform along a tube and so the diameter is constant throughout. This value influences the losses in the flow across a tube bank due to viscous friction.

#### Dependencies

To enable this parameter, set Flow geometry to Flow perpendicular to bank of circular tubes.

Distance between tube centers of the two-phase fluid tubes, aligned with the direction of flow of the moist air.

#### Dependencies

To enable this parameter, set Flow geometry to Flow perpendicular to bank of circular tubes.

Distance between the tube centers in a row of two-phase fluid tubes. This measurement is perpendicular to the moist air flow direction. See Heat Transfer Coefficient for Flows Across a Tube Bank for more information.

#### Dependencies

To enable this parameter, set Flow geometry to Flow perpendicular to bank of circular tubes.

Empirical coefficient for pressure drop across one tube row. The Euler number is the ratio between pressure drop and fluid momentum:

$\text{Eu}=\frac{\Delta p}{N\frac{1}{2}\rho {v}^{2}},$

where N is the Number of tube rows along flow direction, Δp is the pressure drop, ρ is the moist air mixture density, and v is the flow velocity.

Each tube row is located in a plane perpendicular to the moist air flow.

#### Dependencies

To enable this parameter, set Flow geometry to Flow perpendicular to bank of circular tubes and Pressure loss model to Euler number per tube row.

Smallest total flow area between inlet and outlet. If the channel is a collection of ducts, tubes, slots, or grooves, the minimum free-flow area is the sum of the smallest areas.

#### Dependencies

To enable this parameter, set Flow geometry to Generic.

Total area of the heat transfer surface, excluding fins.

#### Dependencies

To enable this parameter, set Flow geometry to Generic.

Total volume of moist air in the heat exchanger.

#### Dependencies

To enable this parameter, set Flow geometry to Generic.

Additional thermal resistance due to fouling layers on the surfaces of the wall. In real systems, fouling deposits grow over time. However, the growth is slow enough to be assumed constant during the simulation.

Total heat transfer surface area of both sides of all fins. For example, if the fin is rectangular, the surface area is double the area of the rectangle.

The total heat transfer surface area is the sum of the channel surface area and the effective fin surface area, which is the product of the Fin efficiency and the Total fin surface area.

Ratio of actual heat transfer to ideal heat transfer through the fins.

Moist air pressure at the start of the simulation.

Temperature in the moist air fluid channel at the start of the simulation. This parameter can be a scalar or a two-element vector. A scalar value represents the mean initial temperature in the channel. A vector value represents the initial temperature at the inlet and outlet in the form [inlet, outlet]. The block calculates a linear gradient between the two ports. The inlet and the outlet ports are identified according to the initial flow direction.

Moisture specification, which can be set as relative humidity, specific humidity, water vapor mole fraction, or humidity ratio.

Relative humidity in the moist air channel at the start of the simulation. The relative humidity is the ratio of the water vapor partial pressure to the water vapor saturation pressure, or the ratio of the water vapor mole fraction to the water vapor mole fraction at saturation.

This parameter can be a scalar or a two-element vector. A scalar value represents the mean initial relative humidity in the channel. A vector value represents the initial relative humidity at the inlet and outlet in the form [inlet, outlet]. The block calculates a linear gradient between the two ports. The inlet and the outlet ports are identified according to the initial flow direction.

#### Dependencies

To enable this parameter, set Initial moisture specification to Relative humidity.

Specific humidity in the moist air channel at the start of simulation. The specific humidity is the mass fraction of water vapor to the combined total mass of water vapor, trace gas, and dry air.

This parameter can be a scalar or a two-element vector. A scalar value represents the mean initial specific humidity in the channel. A vector value represents the initial specific humidity at the inlet and outlet in the form [inlet, outlet]. The block calculates a linear gradient between the two ports. The inlet and the outlet ports are identified according to the initial flow direction.

#### Dependencies

To enable this parameter, set Initial moisture specification to Specific humidity.

Mole fraction of the water vapor in the moist air channel at the start of simulation. The water vapor mole fraction is relative to the combined molar quantity of water vapor, trace species, and dry air.

This parameter can be a scalar or a two-element vector. A scalar value represents the mean initial vapor mole fraction in the channel. A vector value represents the initial vapor mole fraction at the inlet and outlet in the form [inlet, outlet]. The block calculates a linear gradient between the two ports. The inlet and the outlet ports are identified according to the initial flow direction.

#### Dependencies

To enable this parameter, set Initial moisture specification to Mole fraction.

Humidity ratio in the moist air channel at the start of the simulation. The humidity ratio is the ratio of the mass of water vapor to the mass of dry air and trace gas.

This parameter can be a scalar or a two-element vector. A scalar value represents the mean initial humidity ratio in the channel. A vector value represents the initial humidity ratio at the inlet and outlet in the form [inlet, outlet]. The block calculates a linear gradient between the two ports. The inlet and the outlet ports are identified according to the initial flow direction.

#### Dependencies

To enable this parameter, set Initial moisture specification to Humidity ratio.

Measurement type of trace gas.

Amount of trace gas in the moist air channel by mass fraction at the start of the simulation. The mass fraction is relative to the combined total mass of water vapor, trace gas, and dry air.

This parameter can be a scalar or a two-element vector. A scalar value represents the mean trace gas mass fraction in the channel. A vector value represents the initial trace gas mass fraction at the inlet and outlet in the form [inlet, outlet]. The block calculates a linear gradient between the two ports. The inlet and the outlet ports are identified according to the initial flow direction.

This parameter is ignored if the Trace gas model parameter in the Moist Air Properties (MA) block is set to None.

#### Dependencies

To enable this parameter, set Initial trace gas specification to Mass fraction.

Amount of trace gas in the moist air channel by mole fraction at the start of the simulation. The mole fraction is relative to the combined molar total of water vapor, trace gas, and dry air.

This parameter can be a scalar or a two-element vector. A scalar value represents the mean trace gas mole fraction in the channel. A vector value represents the initial trace gas mole fraction at the inlet and outlet in the form [inlet, outlet]. The block calculates a linear gradient between the two ports. The inlet and the outlet ports are identified according to the initial flow direction.

This parameter is ignored if the Trace gas model parameter in the Moist Air Properties (MA) block is set to None.

#### Dependencies

To enable this parameter, set Initial trace gas specification to Mole fraction.

Relative humidity point of condensation. Condensation occurs above this value. A value greater than 1 indicates a supersaturated vapor.

## References

[1] 2013 ASHRAE Handbook - Fundamentals. American Society of Heating, Refrigerating and Air-Conditioning Engineers, Inc., 2013.

[2] Braun, J. E., S. A. Klein, and J. W. Mitchell. "Effectiveness Models for Cooling Towers and Cooling Coils." ASHRAE Transactions 95, no. 2, (June 1989): 164–174.

[3] Çengel, Yunus A. Heat and Mass Transfer: A Practical Approach. 3rd ed, McGraw-Hill, 2007.

[4] Ding, X., Eppe J.P., Lebrun, J., Wasacz, M. "Cooling Coil Model to be Used in Transient and/or Wet Regimes. Theoretical Analysis and Experimental Validation." Proceedings of the Third International Conference on System Simulation in Buildings (1990): 405-411.

[5] Mitchell, John W., and James E. Braun. Principles of Heating, Ventilation, and Air Conditioning in Buildings. Wiley, 2013.

[6] Shah, R. K., and Dušan P. Sekulić. Fundamentals of Heat Exchanger Design. John Wiley & Sons, 2003.

[7] White, Frank M. Fluid Mechanics. 6th ed, McGraw-Hill, 2009.

## Version History

Introduced in R2019a