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Heat exchanger (TH-TH)#

block

Block appearance in REPEAT VISION#

 The block models a heat exchanger in which heat is transferred between two thermal-hydraulic systems. The fluids involved in the heat exchange are single-phase.

 Heat flow calculations are performed using the NTU method. The user can add consideration of the thermal resistance of the wall and deposits on its surfaces.

Equation of conservation of mass (1) :

(1)#\[\dot m_{вх}+\dot m_{вых}=0\]

where \(\dot m_{in},\dot m_{out}\) is the mass flow rate at the inlet and outlet, [kg/s].

Energy conservation equation (2) :

(2)#\[\frac{dE}{dt}=\phi_{вх}+\phi_{вых}-Q\]

where:

 \(E= ho \cdot u \cdot V\) – total internal energy, [J];

 \(\phi_{in},\phi_{out}\) – energy flow at the input and output, [W];

 Q – heat flow, [W].

Equations of conservation of momentum (3) :

(3)#\[p_{вх}-p_{вых}=\Delta p_{вх}-\Delta p_{вых}\]

where:

 \(p_{in},p_{out}\) – pressure at the inlet and outlet of the heat exchanger, [Pa];

 \(\Delta p_{in}=p_{in}-p\) – pressure loss between the inlet and the internal unit, [Pa];

 \(\Delta p_{out}=p_{out}-p\) – pressure loss between the outlet and the internal unit, [Pa];

 p – pressure in the internal node, [Pa].

Calculation of pressure losses in a heat exchanger

 The pressure loss between the block ports and the internal unit is calculated using the following formulas:

(4)#\[\begin{split}p_{вх}^{ср}-p_{вн}^{ср}=\begin{cases}\dot m_{вх} \cdot \mu_{вх}\cdot K_{Потерь} \cdot Re_L \cdot \frac{1}{4\cdot d_г \rho_{вх}\cdot S_{min}}, Re_{вх}\leq Re_L\\K_{Потерь}\cdot \frac{\dot m_{вх}\cdot|\dot m_{вх}|}{4\cdot \rho_{вх}\cdot S_{min}^2}, Re_{вх}\geq Re_T\end{cases}\\ p_{вых}^{ср}-p_{вн}^{ср}=\begin{cases}\dot m_{вх} \cdot \mu_{вых}\cdot K_{Потерь} \cdot Re_L \cdot \frac{1}{4\cdot d_г \rho_{вых}\cdot S_{min}}, Re_{вых}\leq Re_L\\K_{Потерь}\cdot \frac{\dot m_{вых}\cdot|\dot m_{вых}|}{4\cdot \rho_{вых}\cdot S_{min}^2}, Re_{вых}\geq Re_T\end{cases}\end{split}\]

where:

 \(p_{in}^{cp},p_{out}^{cp},p_{in}^{cp}\) – pressure of the medium at the inlet, outlet and in the internal unit, respectively, [Pa];

 \(\dot m_{in},\dot m_{out}\) – mass flow rate of the medium at the inlet and outlet of the heat exchanger, [kg/s];

 \(K_{Losses}\) – pressure loss coefficient;

 \( ho_{in}, ho_{out}\) – density of the medium at the inlet and outlet, [kg/m\(^3\)];

 \(S_{min}\) – minimum cross-sectional area of ​​the flow section, [m\(^2\)];

 \(Re_L\) – upper limit of the Reynolds number for laminar flow;

 \(Re_T\) – lower limit of the Reynolds number for turbulent flow;

 \(\mu_{in},\mu_{out}\) – dynamic viscosity of the medium at the inlet and outlet, [Pa\(\cdot\)s].

(5)#\[\begin{split}p_{вх}^{ср}-p_{вн}^{ср}=\begin{cases}\dot m_{вх} \cdot \mu_{вх}\cdot \lambda \cdot \frac{L+L_{доп}}{4\cdot d_г^2 \rho_{вх}\cdot S_{min}}, Re_{вх}\leq Re_L\\f_{вх}\cdot \frac{(L+L_{доп})\cdot\dot m_{вх}\cdot|\dot m_{вх}|}{4\cdot d_г \cdot \rho_{вх}\cdot S_{min}^2}, Re_{вх}\geq Re_T\end{cases}\\ p_{вых}^{ср}-p_{вн}^{ср}=\begin{cases}\dot m_{вых} \cdot \mu_{вых}\cdot \lambda \cdot \frac{L+L_{доп}}{4\cdot d_г^2 \rho_{вых}\cdot S_{min}}, Re_{вых}\leq Re_L\\f_{вых}\cdot \frac{(L+L_{доп})\cdot\dot m_{вых}\cdot|\dot m_{вых}|}{4\cdot d_г \cdot \rho_{вых}\cdot S_{min}^2}, Re_{вых}\geq Re_T\end{cases}\end{split}\]

where:

 \(L\) – length of the flow path from the inlet to the outlet of the heat exchanger, [m];

 \(L_{add}\) – total equivalent length to take into account additional pressure losses in local resistances, [m];

 \(\lambda\) – form factor for calculating the Darcy friction coefficient in the laminar flow regime;

 \(f_{in},f_{out}\) – Darcy friction coefficient at the input and output.

 The Darcy friction coefficients at the inlet and outlet are calculated using the following formulas (6) :

(6)#\[\begin{split} f_{вх}=\frac{1}{(-1.8 \cdot log_{10} \cdot(\frac{6.9}{Re_{вх}}+(\frac{r}{3.7 \cdot d_г})^{1.11}))^2}\\ f_{вых}=\frac{1}{(-1.8 \cdot log_{10} \cdot(\frac{6.9}{Re_{вых}}+(\frac{r}{3.7 \cdot d_г})^{1.11}))^2} \end{split}\]

where \(r\) is the absolute roughness of the inner surface, [m].

(7)#\[\begin{split}p_{вх}^{ср}-p_{вн}^{ср}=\begin{cases}\dot m_{вх} \cdot \mu_{вх}\cdot \lambda \cdot \frac{L}{4\cdot d_г^2 \rho_{вх}\cdot S_{min}}, Re_{вх}\leq Re_L\\f_{вх} (Re_{вх})\cdot \frac{L}{4\cdot d_г} \cdot\frac{\dot m_{вх}\cdot|\dot m_{вх}|}{\rho_{вх}\cdot S_{min}^2}, Re_{вх}\geq Re_T\end{cases}\\ p_{вых}^{ср}-p_{вн}^{ср}=\begin{cases}\dot m_{вых} \cdot \mu_{вых}\cdot \lambda \cdot \frac{L}{4\cdot d_г^2 \rho_{вых}\cdot S_{min}}, Re_{вых}\leq Re_L\\f_{вых}(Re_{вых})\cdot \frac{L}{4\cdot d_г} \cdot\frac{\dot m_{вых}\cdot|\dot m_{вых}|}{\rho_{вых}\cdot S_{min}^2}, Re_{вых}\geq Re_T\end{cases}\end{split}\]

where \(f_{in}(Re_{in}),f_{out}(Re_{out})\) are the Darcy friction coefficients at the inlet and outlet, calculated on the basis of the tabular data provided by the user, depending on the Reynolds number.

(8)#\[\begin{split}p_{вх}^{ср}-p_{вн}^{ср}=\begin{cases}\dot m_{вх} \cdot \mu_{вх}\cdot Eu(Re_L) \cdot Re_L \cdot \frac{L}{4\cdot d_г \rho_{вх}\cdot S_{min}}, Re_{вх}\leq Re_L\\Eu(Re_{вх})\cdot\frac{\dot m_{вх}\cdot|\dot m_{вх}|}{4\cdot \rho_{вх}\cdot S_{min}^2}, Re_{вх}\geq Re_T\end{cases}\\ p_{вых}^{ср}-p_{вн}^{ср}=\begin{cases}\dot m_{вых} \cdot \mu_{вых}\cdot Eu(Re_L) \cdot Re_L \cdot \frac{L}{4\cdot d_г \rho_{вых}\cdot S_{min}}, Re_{вых}\leq Re_L\\Eu(Re_{вых})\cdot\frac{\dot m_{вых}\cdot|\dot m_{вых}|}{4\cdot \rho_{вых}\cdot S_{min}^2}, Re_{вых}\geq Re_T\end{cases}\end{split}\]

where \(Eu(Re_{in}),Eu(Re_{out})\) are the Euler numbers at the input and output, calculated on the basis of the tabular data provided by the user, depending on the Reynolds number.

Calculation of the heat transfer coefficient

 The heat transfer coefficient is calculated using the following formulas:

(9)#\[h_{ж-ст}=h_{const}\]

where:

 \(h_{l-w}\) – heat transfer coefficient between liquid and wall, [W/(m\(^2 \cdot \)℃)];

 \(h_{const}\) – heat transfer coefficient from the medium to the wall, specified by the user in the block property, [W/(m\(^2 \cdot \)℃)].

 For all other calculation models, the heat transfer coefficient is calculated as the arithmetic mean between the coefficients for the inlet and outlet ports (10) :

(10)#\[h_{ж-ст}=\frac{h_{вх}-h_{вых}}{2}\]

where (11):

(11)#\[\begin{split}h_{вх}=\frac{Nu_{вх}\cdot \lambda_{вх}}{d_{г,т/о}}\\h_{вых}=\frac{Nu_{вых}\cdot \lambda_{вых}}{d_{г,т/о}}\end{split}\]

where:

 \(Nu_{in},Nu_{out}\) – Nusselt number for the input and output ports;

 \(lambda_{in},lambda_{out}\) – thermal conductivity coefficients for the input and output ports, [W/(m\(\cdot\)℃)];

 \(d_{h,h/e}\) – hydraulic diameter for heat exchange calculations, [m], (12):

(12)#\[d_{г,т/о}=\frac{4\cdot S_{min} \cdot L_{т/о}}{S_{т/о}}\]

where:

 \(L_{h/e}\) – characteristic length for heat exchange calculation, [m];

 \(S_{h/e}\) – heat exchange surface area, [m\(^2\)].

Calculation of the Nusselt criterion

(13)#\[\begin{split}Nu_{вх} =\begin{cases}Nu_L,Re_{вх}\leq Re_L \\\frac{(\frac{f_{вх}}{8})\cdot(Re_{вх}-1000)\cdot Pr_{вх}}{1+12.7 \cdot (\frac{f_{вх}}{8})^{1/2} \cdot (Pr_{вх}^{2/3}-1)}, Re_{вх}\geq Re_T\end{cases}\\ Nu_{вых} =\begin{cases}Nu_L,Re_{вых}\leq Re_L \\\frac{(\frac{f_{вых}}{8})\cdot(Re_{вых}-1000)\cdot Pr_{вых}}{1+12.7 \cdot (\frac{f_{вых}}{8})^{1/2} \cdot (Pr_{вых}^{2/3}-1)}, Re_{вых}\geq Re_T\end{cases} \end{split}\]

where:

 \(Nu_L\) – Nusselt number for calculating heat transfer in a laminar flow regime;

 \(Pr_{in},Pr_{out}\) – Prandtl number for the input and output ports;

 \(f_{in},f_{out}\) – friction coefficients calculated using the following formula (14):

(14)#\[f=(0.79 \cdot ln(Re) - 1.64)^{-2}\]
(15)#\[\begin{split}Nu_{вх}=j(Re_{вх, т/о})\cdot Re_{вх, т/о} \cdot Pr_{вх}^{1/3}\\ Nu_{вых}=j(Re_{вых, т/о})\cdot Re_{вых, т/о} \cdot Pr_{вых}^{1/3} \end{split}\]

where:

 \(Re_{in, h/e},Re_{out, h/e}\) – Reynolds numbers for the input and output ports, calculated based on the hydraulic diameter for heat exchange calculations;

 \(j(Re_{вх, т/о}),j(Re_{вых, т/о})\) – числа Колберна на входе и выходе рассчитанные на основе табличных данных, предоставленных пользователем, в зависимости от числа Рейнольдса (16):

(16)#\[\begin{split}Re_{вх, т/о}=\frac{\dot m_{вх}\cdot d_{г,т/о}}{S_{min} \mu_{вх}}\\Re_{вых, т/о}=\frac{\dot m_{вых}\cdot d_{г,т/о}}{S_{min} \mu_{вых}}\end{split}\]
(17)#\[\begin{split}Nu_{вх}=Nu(Re_{вх, т/о}, Pr_{вх})\\Nu_{вых}=Nu(Re_{вых, т/о}, Pr_{вых})\end{split}\]

__ Heat exchange __

 Heat flux by the NTU method (18) :

(18)#\[Q=\epsilon \cdot C_{мин}\cdot (T_{вх}^{ср1} - T_{вх}^{ср2})\]

where:

 \(\epsilon\) – heat exchanger efficiency coefficient;

 \(C_{min}\) – minimum value of \(\dot m_1 \cdot C_{p1}\) and \(\dot m_2 \cdot C_{p2}\), [W/℃];

 \(\dot m_1,\dot m_2\) – mass flow rate of medium 1 and 2, [kg/s];

 \(C_{p1},C_{p2}\) – specific heat capacity of environment 1 and 2, [J/(kg\(\cdot ℃\))];

 \(T_{in}^{cp1},T_{in}^{cp2}\) – temperature of medium 1 and 2 at the inlet to the heat exchanger, [℃].

 Heat exchanger efficiency (19):

(19)#\[\epsilon=\frac{Q}{Q_{макс}}\]

where:

 \(Q\) – actual heat flow, [W];

 \(Q_{max}\) – maximum possible heat flow, [W].

 Formula for calculating the efficiency of a heat exchanger for different mutual movement of the coolant: [1]

Pipe-in-pipe heat exchanger:

Forward flow (20) : [1]

(20)#\[\epsilon = \frac{1 - e^{-NTU\cdot(1+C_{отн})}}{1 + C_{отн}}\]

where:

 NTU - number of heat transfer units;

 \(C_{rel} = \frac{C_{min}}{C_{max}}\).

Counterflow (21) : [1]

(21)#\[\epsilon = \frac{1 - e^{-NTU\cdot(1-C_{отн})}}{1 - C_{отн} \cdot e^{-NTU\cdot(1-C_{отн})}}\]

 For the case \(C_{rel}\) = 1 (22) :

(22)#\[\epsilon = \frac{NTU}{1+NTU}\]

Shell and tube heat exchanger:

  • For the case of one flow of the medium in the housing and 2, 4… flows of the medium in the pipes (23) : [1]

(23)#\[\epsilon_1 = 2 \cdot \{1+C_{отн} + (1+C_{отн}^2)^{1/2}\cdot \frac{1+exp \cdot (-(NTU)_1\cdot (1+C_{отн}^2)^{1/2})}{1-exp \cdot (-(NTU)_1\cdot (1+C_{отн}^2)^{1/2})} \}^{-1}\]

  • For the case of n passages in the housing and 2n, 4n… passages of the medium in the pipes (24) : [1]

(24)#\[\epsilon = ((\frac{1-\epsilon_1 \cdot C_{отн}}{1 - \epsilon_1})^n-1) \cdot ((\frac{1-\epsilon_1 \cdot C_{отн}}{1 - \epsilon_1})^n-C_{отн})^{-1}\]

Cross flow heat exchanger:

  • Both environments are mixed (25) : [1]

(25)#\[\epsilon = \frac{1}{\frac{1}{1-exp \cdot (-NTU)}+\frac{C_{отн}}{1-exp \cdot (-C_{отн} \cdot NTU)}-\frac{1}{NTU}}\]

  • The two environments are immiscible (26) : [1]

(26)#\[\epsilon = 1-exp((\frac{1}{C_{отн}})(NTU)^{0.22} \{exp \cdot (-C_{отн}(NTU)^{0.78})-1 \})\]

  • \(C_{max}\) is miscible - \(C_{min}\) is not miscible (27) : [1]

(27)#\[\epsilon =(\frac{1}{C_{отн}})\cdot (1 - exp \cdot \{ -C_{отн} \cdot(1 - exp \cdot (-NTU))\})\]

  • \(C_{max}\) is not mixed - \(C_{min}\) is mixed (28) : [1]

(28)#\[\epsilon = 1 - exp \cdot (-C_{отн}^{-1}\cdot \{1 - exp \cdot (-C_{отн} \cdot (NTU)) \} )\]

 Number of heat transfer units (29) :

(29)#\[NTU = \frac{1}{C_{мин}\cdot R_{общ}}\]

where \(R_{total}\) is the total thermal resistance between two liquids without taking into account the thermal conductivity of the liquids, [℃/W], (30) :

(30)#\[R_{общ}=\frac{1}{\alpha_1 \cdot A_{ср1}}+\frac{R_{f1}}{A_{ср1}}+ R_{ст} + \frac{R_{f2}}{A_{ср2}} + \frac{1}{\alpha_2 \cdot A_{ср2}}\]

where:

 \(\alpha_1, \alpha_2\) – heat transfer coefficients for environment 1 and 2, [\(\frac{W}{m^2 \cdot ℃}\)];

 \(A_{ср1}, A_{ср2}\) – area of ​​heat exchange surface for environment 1 and 2, [m\(^2\)];

 \(R_{f1},R_{f2}\) – surface contamination coefficients for environments 1 and 2, [\(\frac{m^2 \cdot ℃}{W}\)];

 \(R_{w}\) – thermal resistance of the wall, [\(\frac{℃}{W}\)].

1.  Properties#

Property

Default Value

Description

Units of measurement

Heat exchanger type:
Parallel or counter flow;
Shell and tube;
Cross flow;
Generic - effectiveness table

Parallel or counter flow

-

-

Number of shell passes, available when selecting Heat exchanger type - Shell and tube

1

-

pieces

Cross flow type:
Both fluids mixed;
Both fluids unmixed;
Fluid 1 mixed fluid 2 unmixed;
Fluid 1 unmixed fluid 2 mixed, available when selecting Heat exchanger type - Cross flow

Both fluids mixed

-

-

Number of heat transfer unit vector, available when selecting Heat exchanger type - Generic - effectiveness table

0.5;1.0;2.0;3.0;4.0;5.0;

-

-

Thermal capacity ratio vector, available when selecting Heat exchanger type - Generic - effectiveness table

0.0;0.25;0.5;0.75;1.0;

-

-

Effectiveness table, available when selecting Heat exchanger type - Generic - effectiveness table

\u003C0.3;0.3;0.3;0.3;0.3\u003E
\u003C0.6;0.55;0.5;0.47;0.43\u003E
\u003C0.85;0.76;0.68;0.61;0.55\u003E
\u003C0.94;0.83;0.72;0.65;0.58\u003E
\u003C0.98;0.86;0.75;0.66;0.58\u003E
_\u003C0.99;0.86;0.75;0.66;0.58\u003E

-

-

Wall thermal resistance

1.5E-4

-

°C/W

Minimum free flow area (medium 1)

0.01

-

m\(^2\)

Hydraulic diameter for pressure loss (medium 1)

0.15

-

m

Thermal liquid volume (medium 1)

0.01

-

m\(^3\)

Laminar flow upper Reynolds number limit (medium 1)

2000.0

-

-

Turbulent flow lower Reynolds number limit (medium 1)

4000.0

-

-

Pressure loss model (medium 1):
Pressure loss coefficient;
Correlation for flow inside tubes;
Table - Darcy friction factor vs. Reynolds number;
Table - Euler number vs. Reynolds number

Pressure loss coefficient

-

-

Pressure loss coefficient (medium 1), available when selecting Pressure loss model (medium 1) - Pressure loss coefficient

0.1

-

-

Length of flow path from inlet to outlet (medium 1), available when selecting Pressure loss model (medium 1) - Correlation for flow inside tubes or Table - Darcy friction factor vs. Reynolds number

1.0

-

m

Aggregate equivalent length of local resistance (medium 1), available when selecting Pressure loss model (medium 1) - Correlation for flow inside tubes

0.1

-

m

Internal surface absolute roughness (medium 1), available when selecting Pressure loss model (medium 1) - Correlation for flow inside tubes

1.5E-5

-

m

Reynolds number vector for Darcy friction factor (medium 1), available when selecting Pressure loss model (medium 1) - Table - Darcy friction factor vs. Reynolds number

400.0;1000.0;1500.0;3000.0;4000.0;6000.0;10000.0;
20000.0;40000.0;60000.0;100000.0;1.0E8;

-

-

Darcy friction factor vector (medium 1), available when selecting Pressure loss model (medium 1) - Table - Darcy friction factor vs. Reynolds number

0.264;0.112;0.071;0.0417;0.0387;0.0268;
0.025;0.0232;0.0226;0.022;0.0214;0.0214;

-

-

Laminar friction constant for Darcy friction factor (medium 1), available when selecting Pressure loss model (medium 1) - Correlation for flow inside tubes or Table - Darcy friction factor vs. Reynolds number

64.0

-

-

Reynolds number vector for Euler number (medium 1), available when selecting Pressure loss model (medium 1) - Table - Euler number vs. Reynolds number

400.0;1000.0;1500.0;3000.0;4000.0;6000.0;10000.0;
20000.0;40000.0;60000.0;100000.0;1.0E8;

-

-

Euler number vector (medium 1), available when selecting Pressure loss model (medium 1) - Table - Euler number vs. Reynolds number

4.4505;0.6864;0.4791;0.3755;0.36;0.32;
0.3;0.28;0.26;0.24;0.22;0.2;

-

-

Heat transfer coefficient model (medium 1):
Constant heat transfer coefficient;
Correlation for flow inside tubes;
Table - Colburn factor vs. Reynolds number;
Table Nusselt number vs. Reynolds number and Prandtl number

Constant heat transfer coefficient

-

-

Heat transfer surface area (medium 1)

0.5

-

m\(^2\)

Liquid wall heat transfer coefficient (medium 1), available when selecting Heat transfer coefficient model (medium 1) - Constant heat transfer coefficient

100.0

-

W/(m\(^2 \cdot\)°С)

Length of flow path for heat transfer (medium 1), available when selecting Heat transfer coefficient model (medium 1) - Correlation for flow inside tubes or Table - Colburn factor vs. Reynolds number, or Table Nusselt number vs. Reynolds number and Prandtl number

1.0

-

m

Nusselt number for laminar flow heat transfer (medium 1), available when selecting Heat transfer coefficient model (medium 1) - Correlation for flow inside tubes

3.66

-

-

Reynolds number vector for Colburn factor (medium 1), available when selecting Heat transfer coefficient model (medium 1) - Table - Colburn factor vs. Reynolds number

100.0;150.0;1000.0;

-

-

Colburn factor vector (medium 1), available when selecting Heat transfer coefficient model (medium 1) - Table - Colburn factor vs. Reynolds number

0.019;0.013;0.002;

-

-

Reynolds number vector for Nusselt number (medium 1), available when selecting Heat transfer coefficient model (medium 1) - Table Nusselt number vs. Reynolds number and Prandtl number

100.0;150.0;1000.0;

-

-

Prandtl number vector for Nusselt number (medium 1), available when selecting Heat transfer coefficient model (medium 1) - Table Nusselt number vs. Reynolds number and Prandtl number

1.0;10.0;

-

-

Nusselt number table (medium 1), available when selecting Heat transfer coefficient model (medium 1) - Table Nusselt number vs. Reynolds number and Prandtl number

\u003C3.72;4.21\u003E_\u003C3.75;4.44\u003E_
\u003C4.21;7.15\u003E

-

-

Fouling factor (medium 1)

1.0E-4

-

°С\(\cdot m^2\)/W

Minimum fluid wall heat transfer coefficient (medium 1)

5.0

-

W/(°С\(\cdot m^2\))

Minimum free flow area (medium 2)

0.01

-

m\(^2\)

Hydraulic diameter for pressure loss (medium 2)

0.15

-

m

Thermal liquid volume (medium 2)

0.01

-

m\(^3\)

Laminar flow upper Reynolds number limit (medium 2)

2000.0

-

-

Turbulent flow lower Reynolds number limit (medium 2)

4000.0

-

-

Pressure loss model (medium 2):
Pressure loss coefficient;
Correlation for flow inside tubes;
Table - Darcy friction factor vs. Reynolds number;
Table - Euler number vs. Reynolds number

Pressure loss coefficient

-

-

Pressure loss coefficient (medium 2), available when selecting Pressure loss model (medium 2) - Pressure loss coefficient

0.1

-

-

Length of flow path from inlet to outlet (medium 2), available when selecting Pressure loss model (medium 2) - Correlation for flow inside tubes or Table - Darcy friction factor vs. Reynolds number

1.0

-

m

Aggregate equivalent length of local resistance (medium 2), available when selecting Pressure loss model (medium 2) - Correlation for flow inside tubes

0.1

-

m

Internal surface absolute roughness (medium 2), available when selecting Pressure loss model (medium 2) - Correlation for flow inside tubes

1.5E-5

-

m

Reynolds number vector for Darcy friction factor (medium 2), available when selecting Pressure loss model (medium 2) - Table - Darcy friction factor vs. Reynolds number

400.0;1000.0;1500.0;3000.0;4000.0;6000.0;10000.0;
20000.0;40000.0;60000.0;100000.0;1.0E8;

-

-

Darcy friction factor vector (medium 2), available when selecting Pressure loss model (medium 2) - Table - Darcy friction factor vs. Reynolds number

0.264;0.112;0.071;0.0417;0.0387;0.0268;
0.025;0.0232;0.0226;0.022;0.0214;0.0214;

-

-

Laminar friction constant for Darcy friction factor (medium 2), available when selecting Pressure loss model (medium 2) - Correlation for flow inside tubes or Table - Darcy friction factor vs. Reynolds number

64.0

-

-

Reynolds number vector for Euler number (medium 2), available when selecting Pressure loss model (medium 2) - Table - Euler number vs. Reynolds number

400.0;1000.0;1500.0;3000.0;4000.0;6000.0;10000.0;
20000.0;40000.0;60000.0;100000.0;1.0E8;

-

-

Euler number vector (medium 2), available when selecting Pressure loss model (medium 2) - Table - Euler number vs. Reynolds number

4.4505;0.6864;0.4791;0.3755;0.36;0.32;
0.3;0.28;0.26;0.24;0.22;0.2;

-

-

Heat transfer coefficient model (medium 2):
Constant heat transfer coefficient;
Correlation for flow inside tubes;
Table - Colburn factor vs. Reynolds number;
Table Nusselt number vs. Reynolds number and Prandtl number

Constant heat transfer coefficient

-

-

Heat transfer surface area (medium 2)

0.5

-

m\(^2\)

Liquid wall heat transfer coefficient (medium 2), available when selecting Heat transfer coefficient model (medium 2) - Constant heat transfer coefficient

100.0

-

W/(m\(^2 \cdot\)°С)

Length of flow path for heat transfer (medium 2), available when selecting Heat transfer coefficient model (medium 2) - Correlation for flow inside tubes or Table - Colburn factor vs. Reynolds number, or Table Nusselt number vs. Reynolds number and Prandtl number

1.0

-

m

Nusselt number for laminar flow heat transfer (medium 2), available when selecting Heat transfer coefficient model (medium 2) - Correlation for flow inside tubes

3.66

-

-

Reynolds number vector for Colburn factor (medium 2), available when selecting Heat transfer coefficient model (medium 2) - Table - Colburn factor vs. Reynolds number

100.0;150.0;1000.0;

-

-

Colburn factor vector (medium 2), available when selecting Heat transfer coefficient model (medium 2) - Table - Colburn factor vs. Reynolds number

0.019;0.013;0.002;

-

-

Reynolds number vector for Nusselt number (medium 2), available when selecting Heat transfer coefficient model (medium 2) - Table Nusselt number vs. Reynolds number and Prandtl number

100.0;150.0;1000.0;

-

-

Prandtl number vector for Nusselt number (medium 2), available when selecting Heat transfer coefficient model (medium 2) - Table Nusselt number vs. Reynolds number and Prandtl number

1.0;10.0;

-

-

Nusselt number table (medium 2), available when selecting Heat transfer coefficient model (medium 2) - Table Nusselt number vs. Reynolds number and Prandtl number

\u003C3.72;4.21\u003E_\u003C3.75;4.44\u003E
_\u003C4.21;7.15\u003E

-

-

Fouling factor (medium 2)

1.0E-4

-

°С\(\cdot m^2\)/W

Minimum fluid wall heat transfer coefficient (medium 2)

5.0

-

W/(°С\(\cdot m^2\))

Dynamic compressibility medium 1

Off

-

-

Initial medium 1 temperature

20.0

-

°С

Initial medium gauge pressure (medium 1), available when selecting Dynamic compressibility medium 1 - On

0.0

-

MPa

Dynamic compressibility medium 2

Off

-

-

Initial medium 2 temperature

20.0

-

°С

Initial medium gauge pressure (medium 2), available when selecting Dynamic compressibility medium 2 - On

0.0

-

MPa

2.  Inputs and outputs#

Parameters

Input/Output

Description

Units of measurement

Port type

Medium 1 inlet

Input

-

-

Thermohydraulics

Medium 2 inlet

Input

-

-

Thermohydraulics

Medium 1 outlet

Output

-

-

Thermohydraulics

Medium 2 outlet

Output

-

-

Thermohydraulics

In order to see the connection capabilities of the block, you need to go to page Description of block ports

3.  Sources#

On this page