Plate Condenser Evaporator (TL-2P)

Plate geometry condenser evaporator between two-phase fluid and thermal liquid networks

Since R2024a

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Libraries:
Simscape / Fluids / Heat Exchangers / Two-Phase Fluid - Thermal Liquid

Description

The Plate Condenser Evaporator (TL-2P) block models a plate heat exchanger between a thermal liquid and a two-phase fluid network. The block models the heat transfer between the thermal liquid and the two-phase fluid based on the effectiveness-NTU method. Heat transfer can occur in either direction between the two fluids.

The block uses the Effectiveness-NTU (E-NTU) method to model heat transfer through the shared plate walls. You can also account for heat transfer through the plate itself by selecting the Plate thermal resistance parameter. The block models fouling on the exchanger walls, which increases thermal resistance and reduces the heat exchange between the two fluids.

The two-phase fluid flows use a boundary-following model to track the subcooled liquid, vapor-liquid mixture, and superheated vapor in three zones. The relative amount of space a zone occupies in the system is called a zone fraction.

Plate Heat Exchanger Geometry

Plate heat exchangers consist of a series of clamped-together plates. Each plate has portholes for the fluid to flow through and gaskets around the portholes and the plate sides to contain the liquid. The gasket pattern alternates between the plates so that on each side of the plate, one fluid flows across the plate while the other fluid flows through it. This design results in alternating layers of hot and cold fluid. This figure shows a section of counter-flow in a plate heat exchanger.

This figure shows an individual plate and a cross-section of two adjacent plates. In the individual plate image, the thick lines represent the gaskets and the dotted lines represent the plate corrugation. The block assumes that the flow channel gap between the plates equals the corrugation depth, b.

On this plate, one fluid flows from the top-right port hole across the plate to the bottom-right port hole. The other fluid flows through the gasket on the two left-side portholes and not touch the plate on this side. The plate corrugation patterns increase structural stiffness, surface area, and turbulence.

Because fluid flows along both sides of each plate, the total fluid volume is

$${\text{V}}_{total}=\left(N_p+1\right)b{L}_p{W}_p,$$

where:

• N_p is the value of the Number of plates parameter.

• L_p is the value of the Plate length parameter.

• W_p is the value of the Plate width parameter.

• b is the value of the Spacing between plates parameter.

The volume of each fluid is half of the total volume. The flow cross-sectional area, S, for each fluid is

$$S=\frac{\left(N_p+1\right)}{2}b{W}_p.$$

The total projected surface area of the plates, assuming no corrugation, is

$${\text{A}}_{total,proj}=2N_p{L}_p{W}_p.$$

Each fluid has half of the total heat transfer surface area

$$A_{TL}=A_{2P}=\frac{A_{total,actual}}{2}=\varphi N_p{L}_p{W}_p,$$

where the area enlargement factor, ϕ, accounts for the increased surface area due to the corrugation

$$\varphi =\frac{A_{total,actual}}{A_{total,proj}}=\frac{1+\sqrt{1+{\left(\frac{\pi b}{\lambda }\right)}^2}+4\sqrt{1+{\left(\frac{\pi b}{\sqrt{2}\lambda }\right)}^2}}{6}.$$

The hydraulic diameter for each fluid is

$${\text{D}}_h=\frac{2b}{\varphi }\left(\frac{N_p+1}{N_p}\right).$$

Effectiveness-NTU Heat Transfer

The block calculates the heat transfer rate in three parts to correspond with the with the three fluid zones that occur on the two-phase fluid side of the heat exchanger.

The convective heat transfer in a zone is

$$Q_{zone}=ϵC_{\text{Min}}(T_{\text{In,2P}}-T_{\text{In,TL}}),$$

where:

• C_Min 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, c_p, and the fluid mass flow rate. C_Min is always positive.

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

• T_In,TL is the zone inlet temperature of the thermal liquid.

• ε is the heat exchanger effectiveness.

Effectiveness is a function of the heat capacity rate and the number of transfer units, NTU, and varies based on the heat exchanger flow arrangement. NTU is

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

where:

• z is the individual zone fraction.

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

  $$R=\frac{1}{U_{\text{2P}}{A}_{\text{2P}}}+\frac{F_{\text{2P}}}{A_{\text{2P}}}+R_{\text{W}}+\frac{F_{\text{TL}}}{A_{\text{TL}}}+\frac{1}{U_{\text{TL}}{A}_{\text{TL}}},$$

  where:

  • U is the convective heat transfer coefficient of the respective fluid.

  • F is the value of the Fouling factor parameter on the two-phase fluid or thermal liquid side.

  • R_W is the thermal resistance through the plates. If you select Plate thermal resistance, $${\text{R}}_W=\frac{t}{N_p{L}_p{W}_p{k}_p},$$ where t is the value of the Plate thickness parameter and k_p is the value of the Plate thermal conductivity parameter.

    If you clear the Plate thermal resistance check box, R_W = 0.

The total convective heat transfer rate between the fluids is the sum of the heat transferred in the three zones by the subcooled liquid, Q_L, liquid-vapor mixture, Q_M, and superheated vapor, Q_V,

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

Effectiveness by Flow Arrangement

The heat exchanger effectiveness varies according to the flow configuration and fluid stage. The effectiveness is $$\epsilon =1-\exp (-NTU)$$ for all flow arrangements in the liquid-vapor mixture zone.

For the subcooled liquid and the superheated vapor zones, when Flow arrangement is Parallel flow

$$ϵ=\frac{1-\text{exp}[-NTU(1+C_{\text{R}})]}{1+C_{\text{R}}}.$$

For the subcooled liquid and the superheated vapor zones, when Flow arrangement is Counter flow

$$ϵ=\frac{1-\text{exp}[-NTU(1-C_{\text{R}})]}{1-C_{\text{R}}\text{exp}[-NTU(1-C_{\text{R}})]}.$$

C_R is the ratio between the heat capacity rates of the two fluids

$$C_{\text{R}}=\frac{C_{\text{Min}}}{C_{\text{Max}}}.$$

Conductive Heat Transfer

The conductive heat transfer in a zone is

$$Q_{cond}=\frac{T_{out,TL}-T_{out,2P}}{R_{cond}},$$

where:

• T_out,2P is the zone outlet temperature of the two-phase fluid.

• T_out,TL is the zone outlet temperature of the thermal liquid.

• R_cond is the total conductive thermal resistance between the two flows,

  $$R_{cond}=\frac{D_h}{k_{\text{2P}}{A}_{\text{W,2P}}}+\frac{F_{\text{2P}}}{A_{\text{W,2P}}}+R_{\text{W}}+\frac{F_{TL}}{A_{\text{W,TL}}}+\frac{D_h}{k_{\text{TL}}{A}_{\text{W,TL}}},$$

  where:

  • A_W is the wall surface area.

  • k is the thermal conductivity of each fluid.

  • D_H is the hydraulic diameter.

The total heat transfer is the sum of the convective and conductive heat transfer. The conductive heat transfer is negligible compared to the convective heat transfer. When the flow rate is zero, the convective heat transfer is also zero. However, because heat transfer from convection and conduction operate independently of each other, there is still conductive heat transfer even when the convective heat transfer is zero.

Pressure Loss

For both fluids and pressure loss parameterizations, the pressure loss between each port and the internal node is

$$\begin{array}{l}{\text{p}}_A-p_I=\frac{{\xi }_{ports}{\dot{m}}_A\left|{\dot{m}}_A\right|}{4\rho S_{port,A}^2}+\frac{f_{Darcy}{L}_p{\dot{m}}_A\left|{\dot{m}}_A\right|}{4\rho D_h{S}^2}\\ {\text{p}}_B-p_I=\frac{{\xi }_{ports}{\dot{m}}_B\left|{\dot{m}}_B\right|}{4\rho S_{port,B}^2}+\frac{f_{Darcy}{L}_p{\dot{m}}_B\left|{\dot{m}}_B\right|}{4\rho D_h{S}^2}\end{array}$$

where:

• ṁ_A is the mass flow rate through port A1 or A2 when the block calculates the values for the thermal liquid and two-phase networks, respectively.

• ṁ_B is the mass flow rate through port A1 or A2 when the block calculates the values for the thermal liquid and two-phase networks, respectively.

• ρ is the fluid density.

• ξ_ports is the value of the Loss coefficient for inlet and outlet manifolds and ports parameter.

• S_port,A is the value of the Cross-sectional area at port A1 or Cross-sectional area at port A2 parameter, when the block calculates the values for the thermal liquid and two-phase networks, respectively.

• S_port,B is the value of the Cross-sectional area at port B1 or Cross-sectional area at port B2 parameter, when the block calculates the values for the thermal liquid and two-phase networks, respectively.

When the Pressure loss model parameter is Friction factor, you use the Darcy friction factor for flow between corrugated plates parameter to specify a single constant friction factor for the fluid. f_Darcy is the value of the Darcy friction factor for flow between corrugated plates parameter.

When the Pressure loss model parameter is Correlation for flow between corrugated plates, the block calculates the Darcy friction factor based on the plate geometry data and Reynolds number from [3].

The Reynolds number is $$\text{Re=}\frac{\dot{m}{D}_h}{\mu S},$$ where μ is the dynamic viscosity. When the Reynolds number is between 200 and 1000,

$$f_{Darcy}={\left[\frac{\text{cos}\beta }{\sqrt{0.18\tan \beta +0.36\sin \beta +\frac{64}{Re\text{cos}\beta }}}+\frac{1-\text{cos}\beta }{\sqrt{3.8\left(\frac{597}{Re}+3.85\right)}}\right]}^{-2}.$$

When the Reynolds number is greater than 2000,

$$f_{Darcy}={\left[\frac{\text{cos}\beta }{\sqrt{0.18\tan \beta +0.36\sin \beta +\frac{1}{{\left(1.8\ln Re-1.5\right)}^2\text{cos}\beta }}}+\frac{1-\text{cos}\beta }{\sqrt{\frac{3.8\ast 39}{{\mathrm{Re}}^{0.289}}}}\right]}^{-2}.$$

The block uses a smooth cubic transition between these regions and for Reynolds numbers between 1000 and 2000. For Reynolds numbers below 200, the block calculates f_Darcy from a laminar friction constant that ensures numerical robustness as the flow goes to 0.

Heat Transfer Coefficient

The heat transfer coefficient, U, is

$$U=Nu\frac{k}{D_h}.$$

The heat transfer calculations depend on the value of the Heat transfer coefficient model parameter and the two-phase fluid zone. When the thermal liquid and two-phase fluid are in the subcooled liquid or superheated vapor zone, k is the fluid thermal conductivity. When the two-phase fluid is in the saturated liquid-vapor mixture zone, k is the saturated liquid thermal conductivity.

Colburn Equation

When Heat transfer coefficient model is Colburn equation, the block calculates the heat transfer coefficient from data by using the Colburn correlation coefficients.

When the thermal liquid and two-phase fluid are in the subcooled liquid or superheated vapor zone, the Nusselt number is

$$Nu=aR{e}^{b}P{r}^c,$$

where a, b, and c are the first, second, and third elements in the Coefficients [a, b, c] for a*Re^b*Pr^c parameter and Pr is the Prandtl number.

When the two-phase fluid is in the saturated liquid-vapor mixture zone, the Nusselt number from [2] is

$$Nu=\frac{a\varphi R{e}_{SL}^{b}P{r}_{SL}^c\left\{{\left[\left(\sqrt{\frac{v_{SV}}{v_{SL}}-1}\right)x_{out}+1\right]}^{1+b}-{\left[\left(\sqrt{\frac{v_{SV}}{v_{SL}}-1}\right)x_{in}+1\right]}^{1+b}\right\}}{\left(1+b\right)\left(\sqrt{\frac{v_{SV}}{v_{SL}}-1}\right)\left(x_{out}-x_{in}\right)},$$

where:

• Re_SL and Pr_SL are the Reynolds number and the Prandtl number of the saturated liquid, respectively.

• v_SL and v_SV are the saturated liquid and vapor specific volumes, respectively.

• x_in is the vapor quality at the start of the saturated liquid-vapor mixture zone.

• x_out is the vapor quality at the end of the saturated liquid-vapor mixture zone.

Correlation for Flow Between Corrugated Plates

When Heat transfer coefficient model is Correlation for flow between corrugated plates, the block calculates the heat transfer coefficient based on the plate geometry data.

When the thermal liquid and two-phase fluid are in the subcooled liquid or superheated vapor zone, the Nusselt number from [3] is

$$Nu=c_1{\left(f_{Darcy}R{e}^2\sin 2\beta \right)}^{c_2}{\mathrm{Pr}}^{c_3},$$

where:

• c₁, c₂, and c₃ are the first, second, and third elements in the Coefficients for Martin correlation parameter.

• Pr is the Prandtl number.

When the two-phase fluid is in the saturated liquid-vapor mixture zone, the Nusselt number from [2] is

$$Nu=\frac{c_1\varphi R{e}_{SL}^{c_2}P{r}_{SL}^{c_3}\left\{{\left[\left(\sqrt{\frac{v_{SV}}{v_{SL}}-1}\right)x_{out}+1\right]}^{1+c_2}-{\left[\left(\sqrt{\frac{v_{SV}}{v_{SL}}-1}\right)x_{in}+1\right]}^{1+c_2}\right\}}{\left(1+c_2\right)\left(\sqrt{\frac{v_{SV}}{v_{SL}}-1}\right)\left(x_{out}-x_{in}\right)}.$$

Conservation Equations

Two-Phase Fluid

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

$$\frac{d{M}_{\text{2P}}}{dt}={\dot{m}}_{\text{A2}}+{\dot{m}}_{\text{B2}},$$

where:

• M_2P is the total mass of the two-phase fluid.

• $$\dot{m}$$_A2 is the mass flow rate of the fluid at port A2.

• $$\dot{m}$$_B2 is the mass flow rate of the fluid at port B2.

The block relates the change in specific internal energy to the heat transfer by the fluid by using the equation

$$M_{2P}\frac{d{u}_{2P}}{dt}+u_{2P}\left({\dot{m}}_{A2}+{\dot{m}}_{B2}\right)={\varphi }_{\text{A2}}+{\varphi }_{\text{B2}}+Q,$$

where:

• u_2P is the two-phase fluid specific internal energy.

• φ_A1 is the energy flow rate at port A1.

• φ_B1 is the energy flow rate at port B1.

• Q is heat transfer rate.

Thermal Liquid

The total mass accumulation rate in the thermal liquid is

$$\frac{d{M}_{\text{TL}}}{dt}={\dot{m}}_{\text{A1}}+{\dot{m}}_{\text{B1}}.$$

The energy conservation equation is

$$M_{TL}\frac{d{u}_{TL}}{dt}+u_{TL}\left({\dot{m}}_{A1}+{\dot{m}}_{B1}\right)={\varphi }_{\text{A1}}+{\varphi }_{\text{B1}}-Q,$$

where:

• ϕ_A1 is the energy flow rate at port A1.

• ϕ_B1 is the energy flow rate at port B1.

The heat transferred to or from the thermal liquid, Q, equals the heat transferred from or to the two-phase fluid.

Ports

Output

Z — Liquid, mixture, and vapor zone fractions, unitless

physical signal

Physical signal output port that measures the liquid, mixture, and vapor zone fractions in the heat exchanger.

Conserving

A1 — Thermal liquid inlet or outlet

thermal liquid

Inlet or outlet port associated with the thermal liquid.

B1 — Thermal liquid inlet or outlet

thermal liquid

Inlet or outlet port associated with the thermal liquid.

A2 — Two-phase inlet or outlet

two-phase fluid

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

B2 — Two-phase inlet or outlet

two-phase fluid

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

Parameters

Configuration

Flow arrangement — Flow path alignment

Counter flow (default) | Parallel flow

Flow path alignment across the heat exchanger. 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.

Number of plates — Number of plates in heat exchanger

25 (default) | positive scalar

Number of plates in the heat exchanger. Fluid flows across both sides of each plate, including the end plate and start plate.

Plate length — Length of plates

1 m (default) | positive scalar

Length of each plate. This value is the longer side of the plate and the flow axis of the fluid.

Plate width — Width of plates

0.5 m (default) | positive scalar

Width of each plate.

Spacing between plates — Space between plates

5e-3 m (default) | positive scalar

Gap between each plate. This parameter value usually equals the corrugation depth.

Corrugation pattern specification — Option for specifying corrugation pattern

Surface area enlargement factor (default) | Chevron geometry

Whether you specify the surface area enlargement factor directly or the block calculates the enlargement factor from a specified chevron geometry.

Surface area enlargement factor — Multiplier that accounts for increased plate area

1.17 (default) | positive scalar

Multiplier that accounts for the increase in plate surface area due to corrugation. If each plate is perfectly flat, the value of this parameter is 1. Otherwise, this value is the ratio of the actual total surface area to the area of the two-dimensional projection of the plate shape.

Dependencies

To enable this parameter, set Corrugation pattern specification to Surface area enlargement factor.

Corrugation chevron angle — Angle of chevron on plate

60 deg (default) | positive scalar

Angle of the chevron corrugation on each plate. This value is β in this plate diagram:

Dependencies

To enable this parameter, set Corrugation pattern specification to Chevron geometry.

Corrugation depth to pitch ratio — Ratio of chevron depth to pitch

0.28 (default) | positive scalar

Ratio of the chevron corrugation depth to the corrugation pitch. The corrugation pitch is the corrugation wavelength. The value of this parameter is b/λ in this diagram:

Dependencies

To enable this parameter, set Corrugation pattern specification to Chevron geometry.

Plate thermal resistance — Option to model plate thermal resistance

off (default) | on

Option to model plate thermal resistance. If you select this check box, the block uses the values of the Plate thickness and Plate thermal conductivity parameters to calculate the thermal resistance through each plate. If you clear this check box, the block does not model the effects of thermal resistance through the plates.

Plate thickness — Thickness of plates

5e-4 m (default) | positive scalar

Thickness of each plate in the heat exchanger.

Dependencies

To enable this parameter, select Plate thermal resistance.

Plate thermal conductivity — Thermal conductivity through plate

15 W/(K*m) (default) | positive scalar

Thermal conductivity of each plate.

Dependencies

To enable this parameter, select Plate thermal resistance.

Cross-sectional area at port A1 — Flow area at port A1

0.01 m^2 (default) | positive scalar

Flow area at the thermal liquid port A1.

Cross-sectional area at port B1 — Flow area at port B1

0.01 m^2 (default) | positive scalar

Flow area at the thermal liquid port B1.

Cross-sectional area at port A2 — Flow area at port A2

0.01 m^2 (default) | positive scalar

Flow area at the two-phase fluid port A2.

Cross-sectional area at port B2 — Flow area at port B2

0.01 m^2 (default) | positive scalar

Flow area at the two-phase fluid port B2.

Thermal Liquid 1

Pressure loss model — Method of pressure loss calculation from viscous friction

Correlation for flow between corrugated plates (default) | Friction factor

Method of pressure loss calculation due to viscous friction for the thermal liquid. The settings are:

• Friction factor — The block calculates the pressure loss based on a constant Darcy friction factor for flow between the plate passages, specified by the Darcy friction factor for flow between corrugated plates parameter.

• Correlation for flow between corrugated plates — The block uses the Martin correlation for plate heat exchangers with the chevron or herringbone pattern to calculate the pressure loss.

Darcy friction factor for flow between corrugated plates — Constant Darcy friction factor

1.7 (default) | positive scalar

Constant Darcy friction factor to use to calculate the pressure loss.

If you have data for the pressure loss across the heat exchanger, Δp_data, and the mass flow rate through the heat exchanger, ṁ_data, the value of this parameter is

$$f_{darcy}=\frac{D_h{S}^2}{L_p}\left[2\rho \left(\frac{\Delta p_{data}}{{\dot{m}}_{data}^2}\right)-\frac{{\xi }_{ports}}{S_{port}}\right].$$

If you do not have data for ξ_ports, use the default value of the Loss coefficient for inlet and outlet manifolds and ports parameter in this expression. If you have multiple data points for Δp_data and ṁ_data, use a least squares fit to find f_darcy.

If you know the loss coefficient value, ξ_loss, for your heat exchanger, then f_Darcy = ξ_loss D_h / L_P.

Dependencies

To enable this parameter, set Pressure loss model to Friction factor.

Loss coefficient for inlet and outlet manifolds and ports — Pressure loss coefficient for inlet and outlet manifolds and ports

1.5 (default) | positive scalar

Pressure loss coefficient that accounts for losses at the inlet and outlet manifolds and ports on the thermal liquid side.

Heat transfer coefficient model — Method of calculating heat transfer coefficient

Correlation for flow between corrugated plates (default) | Colburn equation

Method of calculating the heat transfer coefficient for the thermal fluid. The available settings are:

• Colburn equation — Use this setting to calculate the heat transfer coefficient by defining the variables a, b, and c of the Colburn equation. Use this option to fit the heat transfer results to the experimental data by estimating the coefficients.

• Correlation for flow between corrugated plates — Use this setting to calculate the heat transfer coefficient based on the plate geometry data and the Martin correlation.

Coefficients [a, b, c] for a*Re^b*Pr^c — Colburn equation coefficients

[.141, .748, .333] (default) | three-element vector

Three-element vector that contains the empirical coefficients of the Colburn equation. The Colburn equation is a formulation for calculating the Nusselt number.

Dependencies

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

Coefficients for Martin correlation — Martin correlation coefficients

[.122, .374, .333] (default) | three-element vector

Three-element vector that contains the coefficients c₁, c₂, and c₃ that the block uses to calculate the Nusselt number by using the Martin correlation:

$${\text{Nu=c}}_1{\left(f_{Darcy}{\mathrm{Re}}^2\sin 2\beta \right)}^{c_2}{\mathrm{Pr}}^{c_3}.$$

Dependencies

To enable this parameter, set Heat transfer coefficient model to Correlation for flow between corrugated plates.

Fouling factor — Thermal resistance from fouling deposits

0.1 K*m^2/kW (default) | positive scalar

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 that the block assumes the fouling is constant during the simulation.

Initial thermal liquid pressure — Thermal liquid pressure at start of simulation

0.101325 MPa (default) | positive scalar

Thermal liquid pressure at the start of the simulation.

Initial thermal liquid temperature — Thermal liquid temperature at start of simulation

293.15 K (default) | positive scalar | two-element vector

Temperature in the thermal liquid 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 fluid flow. 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 initial flow direction determines the inlet and outlet ports.

Two-Phase Fluid 2

Pressure loss model — Method of pressure loss calculation from viscous friction

Correlation for flow between corrugated plates (default) | Friction factor

Method of pressure loss calculation due to viscous friction for the two-phase fluid. The settings are:

• Friction factor — The block calculates the pressure loss based on a constant Darcy friction factor for flow between the plate passages, specified by the Darcy friction factor for flow between corrugated plates parameter.

• Correlation for flow between corrugated plates — The block uses the Martin correlation for plate heat exchangers with the chevron or herringbone pattern to calculate the pressure loss.

Darcy friction factor for flow between corrugated plates — Constant Darcy friction factor

1.7 (default) | positive scalar

Constant Darcy friction factor to use to calculate the pressure loss.

If you have data for the pressure loss across the heat exchanger, Δp_data, and the mass flow rate through the heat exchanger, ṁ_data, the value of this parameter is

$$f_{darcy}=\frac{D_h{S}^2}{L_p}\left[2\rho \left(\frac{\Delta p_{data}}{{\dot{m}}_{data}^2}\right)-\frac{{\xi }_{ports}}{S_{port}}\right].$$

If you do not have data for ξ_ports, use the default value of the Loss coefficient for inlet and outlet manifolds and ports parameter in this expression. If you have multiple data points for Δp_data and ṁ_data, use a least squares fit to find f_darcy.

If you know the loss coefficient value, ξ_loss, for your heat exchanger, then f_Darcy = ξ_loss D_h / L_P.

Dependencies

To enable this parameter, set Pressure loss model to Friction factor.

Loss coefficient for inlet and outlet manifolds and ports — Pressure loss coefficient for inlet and outlet manifolds and ports

1.5 (default) | positive scalar

Pressure loss coefficient that accounts for losses at the inlet and outlet manifolds and ports on the thermal liquid side.

Heat transfer coefficient model — Method of calculating heat transfer coefficient

Correlation for flow between corrugated plates (default) | Colburn equation

Method of calculating the heat transfer coefficient for the two-phase fluid. The available settings are:

• Colburn equation — Use this setting to calculate the heat transfer coefficient by defining the variables a, b, and c of the Colburn equation. Use this option to fit the heat transfer results to the experimental data by estimating the coefficients.

• Correlation for flow between corrugated plates — Use this setting to calculate the heat transfer coefficient based on the plate geometry data and the Martin correlation.

Coefficients [a, b, c] for a*Re^b*Pr^c in liquid zone — Colburn equation coefficients in liquid zone

[.141, .748, .333] (default) | three-element vector

Three-element vector that contains the empirical coefficients of the Colburn equation. Each fluid zone has a distinct Nusselt number, which the block calculates by using the Colburn equation in each 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.

Coefficients [a, b, c] for a*Re^b*Pr^c in mixture zone — Longo correlation equation coefficients in mixture zone

[1.875, .445, .333] (default) | three-element vector

Three-element vector that contains the coefficients for the Longo correlation. The block uses the Longo correlation to calculate the Nusselt number in the mixture zone.

Dependencies

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

Coefficients [a, b, c] for a*Re^b*Pr^c in vapor zone — Colburn equation coefficients in vapor zone

[.141, .748, .333] (default) | three-element vector

Three-element vector that contains the empirical coefficients of the Colburn equation. Each fluid zone has a distinct Nusselt number, which the block calculates by using the Colburn equation in each 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.

Coefficients for Martin correlation in liquid zone — Martin equation coefficients in liquid zone

[.122, .374, .333] (default) | three-element vector

Three-element vector that contains the coefficients c₁, c₂, and c₃ that the block uses to calculate the Nusselt number by using the Martin correlation in the liquid zone:

$${\text{Nu=c}}_1{\left(f_{Darcy}{\mathrm{Re}}^2\sin 2\beta \right)}^{c_2}{\mathrm{Pr}}^{c_3}.$$

Dependencies

To enable this parameter, set Heat transfer coefficient model to Correlation for flow between corrugated plates.

Coefficients for Longo correlation in mixture zone — Longo correlation equation coefficients in mixture zone

[1.875, .445, .333] (default) | three-element vector

Three-element vector that contains the coefficients for the Longo correlation. The block uses the Longo correlation to calculate the Nusselt number in the mixture zone.

Dependencies

To enable this parameter, set Heat transfer coefficient model to Correlation for flow between corrugated plates.

Coefficients for Martin correlation in vapor zone — Martin equation coefficients in vapor zone

[.122, .374, .333] (default) | three-element vector

Three-element vector that contains the coefficients c₁, c₂, and c₃ that the block uses to calculate the Nusselt number by using the Martin correlation in the vapor zone:

$${\text{Nu=c}}_1{\left(f_{Darcy}{\mathrm{Re}}^2\sin 2\beta \right)}^{c_2}{\mathrm{Pr}}^{c_3}.$$

Dependencies

To enable this parameter, set Heat transfer coefficient model to Correlation for flow between corrugated plates.

Fouling factor — Thermal resistance from fouling deposits

0.1 K*m^2/kW (default) | positive scalar

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 that the block assumes the fouling is constant during the simulation.

Initial fluid energy specification — Initial state of two-phase fluid

Temperature (default) | Vapor quality | Vapor void fraction | Specific enthalpy | Specific internal energy

Quantity used to describe the initial state of the fluid.

The value for Initial fluid energy specification parameter limits the available initial states for the two-phase fluid. When Initial fluid energy specification is:

• Temperature — Specify an initial state that is a subcooled liquid or superheated vapor. You cannot specify a liquid-vapor mixture because the temperature is constant across the liquid-vapor mixture region.

• Vapor quality — Specify an initial state that is a liquid-vapor mixture. You cannot specify a subcooled liquid or a superheated vapor because the liquid mass fraction is 0 and 1, respectively, across the whole region. Additionally, the block limits the pressure to below the critical pressure.

• Vapor void fraction — Specify an initial state that is a liquid-vapor mixture. You cannot specify a subcooled liquid or a superheated vapor because the liquid mass fraction is 0 and 1, respectively, across the whole region. Additionally, the block limits the pressure to below the critical pressure.

• Specific enthalpy — Specify the specific enthalpy of the fluid. The block does not limit the initial state.

• Specific internal energy — Specify the specific internal energy of the fluid. The block does not limit the initial state.

Initial two-phase fluid pressure — Fluid pressure at start of simulation

0.101325 MPa (default) | positive scalar

Fluid pressure at the start of the simulation.

Initial two-phase fluid temperature — Temperature at start of simulation

293.15 K (default) | positive scalar | two-element vector

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 initial flow direction determines the inlet and outlet ports.

Dependencies

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

Initial two-phase fluid vapor quality — Vapor mass fraction at start of simulation

0.5 (default) | positive scalar in the range [0,1] | two-element vector in the range [0,1]

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 initial flow direction determines the inlet and outlet ports.

Dependencies

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

Initial two-phase fluid vapor void fraction — Vapor volume fraction at start of simulation

0.5 (default) | positive scalar in the range [0,1] | two-element vector in the range [0,1]

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 initial flow direction determines the inlet and outlet ports.

Dependencies

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

Initial two-phase fluid specific enthalpy — Enthalpy per unit mass at start of simulation

1500 kJ/kg (default) | positive scalar | two-element vector

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 initial flow direction determines the inlet and outlet ports.

Dependencies

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

Initial two-phase fluid specific internal energy — Internal energy at start of simulation

1500 kJ/kg (default) | positive scalar | two-element vector

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 initial flow direction determines the inlet and outlet ports.

Dependencies

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

References

[1] Shah, Ramesh K., and Dusan P. Sekulic. Fundamentals of heat exchanger design. John Wiley & Sons, 2003.

[2] Longo, Giovanni A., Giulia Righetti, and Claudio Zilio. "A new computational procedure for refrigerant condensation inside herringbone-type Brazed Plate Heat Exchangers." International Journal of Heat and Mass Transfer 82 (2015): 530-536.

[3] Martin, Holger. "A theoretical approach to predict the performance of chevron-type plate heat exchangers." Chemical Engineering and Processing: Process Intensification 35.4 (1996): 301-310.

Extended Capabilities

C/C++ Code Generation
Generate C and C++ code using Simulink® Coder™.

Version History

Introduced in R2024a