Component 126: Transient Heat Exchanger

In This Topic

Component 126 : Transient heat exchanger

Specifications

Line connections
1	Fluid inlet primary
2	Fluid outlet primary
3	Fluid inlet secondary
4	Fluid outlet secondary

General User Input Values Results Characteristic Lines Physics Used Displays Examples

General

Component 126 is mainly based on Component 119 (Indirect storage). The expansion consists in the fact that a second fluid (secondary side) is introduced into the calculation mesh. It is in thermal contact with the storage and thus also with fluid 1 (primary side). The influence of the flow type and the geometry of the real structure on the heat transmission are considered by the heat transfer coefficients. They are specified for the transfer surfaces between the walls and the outside wall of the fluid. The basic pattern thus follows the concept of a double-pipe heat exchanger with respect to following scheme:

A modeling equivalent to the pipe has the advantage that a large number of technical applications can be related to the theory of heat transfer in pipes. Another advantage of the pipe geometry is the cycle-symmetric temperature distribution and heat transfer, so that the calculation of the temperature field is reduced to one radial component over the profiles (y-axis of the calculation mesh) and one along the direction of flow (x-axis of the calculation mesh).

The transient heat conduction in the separation wall between the fluids as well as in the outer boundary wall becomes numerical, calculated with the Crank-Nicolson algorithm analogously to Component 119. The overall balance equation gets in comparison to steady state heat exchangers an extension in terms of sinks and sources as shown in next formula:

Please see also chapter 2.2 in "Physics Used".
For t -> infinite, the exchanged amounts of heat will reach the values of the steady state case, what means that the 3 characteristic equations used for calculating heat transfer a valid again::

Q12 (primary) M12 cp12 (T2-T1),or M12 h12
Q34 (secondary): M34 cp34 (T3-T4), or M34 h34
Qtrans: kA dTlog

This system of equations is going to be solved during all calculations in order to get the steady state solution asMacro (partial mode) --> Insert... a long term asymptote. This means always accordance to other steady state results.

This transient module is in equivalence to component 119 also controlled by the time series dialogue.

There are three macros (partial models), which demonstrate the usage of this component. You can insert them in your model by clicking on the menu entry "Insert --> Macro (partial mode) --> Insert...". Then select one of the entries "Transient heating surface", "Transient heating surface shape 2" or "Transient heating surface shape 3". After inserting the macro into your model, open the macro to inspect its data. In order to be able to calculate with this, boundary values (component 1) must be connected to the open line inputs and a time series must be created.

User Input Values

FMODE	Flag for calculation mode Design/Off-design =0: Global =1: local off-design (i.e. always off-design mode, even when a design calculation has been done globally) =2: special local off-design (Special case for compatibility with the earlier Ebsilon-versions, should not be used in new models, because the results of the real off-design calculations are not always consistent) = -1: local design (i.e. always design mode, even when a off-design calculation has been done globally)
FINIT	Flag: Initializing state =0: GLOBAL controlled by variable "Transient mode" in Model Options "Extras" ->"Model Options" -> "Simulation" -> "Transient" -> Combo Box "Transient mode" =1: First run -> Initializing while calculating steady state values =2: Continuation run -> Values from previous time step are input for the present ones
FINST	Flag: Transient calculation mode =0: Transient solution according to time series table =1: Always stationary solution
FFU	Flag: On-/off-switch =0: Heat exchanger off (Only calculation of pressure drops) =1: Heat exchanger on
AWF13	Heat transfer area of separation (bridge) wall
FVOL	Flag: Part-load pressure drop, consideration of mass and or volume =0: without influence of volume DP/DPN = (M/MN)*2 =1: with influence of volume DP/DPN = V/VN(M/MN)**2 < =2: constant (independent from load) DP = DPN
FDPNUM	Pressure loss handling in the numerical solution =0: Using the average fluid pressure between inlet and outlet =1: Use of a linear pressure distribution between inlet and outlet, corresponding pressure values in the individual NFLOW fluid elements
FDP12RN	Flag for the type of definition of the primary pressure loss =1: absolute (DP12N=DP12RN) =2: relative (DP12N=P1N*DP12RN) =-1: P2 given from outside
DP12RN	Pressure loss 12 (nominal) [absolute or relative to P1]
FDP34RN	Flag for the type of definition of the primary pressure loss =1: absolute =2: relative (DP34N=P3N*DP34RN) = -1: P4 given from outside
DP34RN	Pressure loss 34 (nominal) [absolute or relative to P3]
FALPH12	Flag: Determination of the heat transfer coefficient alpha for primary fluid to separation wall =0: always constant value AL12N =1: calculated from AL12 = AL12N(M1/M1N*EX12) =2: calculated using a free defined kernel expression EAPLH12
AL12N	Heat transfer coefficient alpha for primary fluid to separation wall (nominal, only visible if FALPH12 = 0\|1) ) As a first guess these values are recommended: AL12N_WATER=6000 W/(m²K) AL12N_STEAM=500 W/(m²K)
EX12	Exponent for heat transfer coefficient to calculate AL12 AL12 = AL12N(M1/M1N*EX12)
EALPH12	Function for calculation of AL12, equals return value of evalexpr (type real)
FALPH34	Flag: Determination of the heat transfer coefficient alpha for secondary fluid to separation wall =0: always constant value AL34N =1: calculated from AL34 = AL34N(M3/M3N*EX34) =2: calculated using a free defined kernel expression EAPLH34
AL34N	Heat transfer coefficient alpha for secondary fluid to separation wall (nominal, only visible if FALPH34 = 0\|1) ) As a first guess these value is recommended: AL34N_Gas=50 W/(m²K)
EX34	Exponent for heat transfer coefficient to calculate AL34 AL34 = AL34N(M3/M3N*EX34)
EALPH34	Function for calculation of AL12, equals return value of evalexpr (type real)
FALPHO	Flag: Determination of alpha outside =0: From constant value ALPHO =1: From function EALPHO
ALPHO	Outer heat transfer coefficient (to ambient)
EALPHO	Function for calculation of ALPHO, equals return value of evalexpr (type real)
THISO	Thickness of insulation
LAMISO	Heat conductivity of insulation
FALGINST	Flag: Switch for transient calculation modes =1: Crank-Nicolson-Algorithm =4: reduced physical model
FFLOW	Flag: flow direction =0: Counter Current =1: Concurrent (not in design mode)
TAUADBW	Correction factor for time constant of the bridge wall (reduced physical model only)
TAUADOW	Correction factor for time constant of the outer wall (reduced physical model only)
LAMADJ	Multiplication factor to 1/LAMBDA - the walls heat conductivity resistance (reduced physical model only) Setting LAMADJ=0 is equivalent to neglecting the walls heat conductivity resistance: either the wall thickness is infinitely small or lambda value is infinitely high Setting LAMADJ=1 is equivalent to computing the walls heat conductivity with the original value of LAMBDA and wall thickness LAMADJ<1 leads to decreasing the walls heat conductivity resistance LAMADJ>1 leads to increasing the walls heat conductivity resistance
FADAPT	Flag: Switch for using adaption polynomial ADAPT / adaptation function EADAPT = 0: Not used and not evaluated = 1: Correction for kA [KA = KAN K/KN * polynomial] = 2: Calculation of kA [KA = KAN polynomial] = 1000: Polynomial not used, but ADAPT evaluated as RADAPT (Reduction of the computing time) = -1: Correction for kA [KA = KAN K/KN * adaptation function] = -2: Calculation of kA [ KA = KAN adaptation function ] = -1000: Adaptation function not used, but EADAPT evaluated as RADAPT (Reduction of the computing time)
EADAPT	Input of Adaptation-Function
TOLXECO	Tolerance for evaporation in an economizer. If the steam content X at the economizer outlet is > TOLXECO, a warning message is issued. If it is > 2*TOLXECO, an error message is issued.
PINPMIN	Minimum value for the pinch point (KA is reduced automatically if the pinch point would fall below this value)
LSTO12	Length of primary flow FLUID12
LSTO34	Length of secondary flow FLUID34
AWOUT	Heat exchanging area of outer wall
MWF13	Mass of separation wall between fluids (bridge wall)
MWOUT	Mass of outer wall
FVFLUID	Flag: Switch for calculation of fluid volumes =0: Given from specifications VFLUID12, VFLUID34 =1: Given from geometry of the heat exchanger -> pipe geometry with circular cross section
VFLUID12	Volume of primary FLUID12
VFLUID34	Volume of secondary FLUID34
FDATABW	Flag: Property data source and interpolation =1: Constant from specification values RHOBW, LAMBW und CPBW =2: Linear from specification values RHOBW/DRHOBW, LAMBW/DLAMBW und CPBW/DCPBW The values dependent on the separation wall temperature TBW are computed as RHO(TBW) = RHOBW + (TBW - TREFBW)DRHOBW LAM(TBW) = LAMBW + (TBW - TREFBW)DLAMBW CP(TBW) = CPBW + (TBW - TREFBW)DCPBW =3: From characteristic lines <CRHOBW, CLAMBW, CCPBW*
RHOBW	Density of bridge wall at TREFBW
DRHOBW	Density change per degree of separation wall
LAMBW	Heat conductivity of bridge wall at TREFBW
DLAMBW	Heat conductivity change per degree of bridge wall
CPBW	Specific heat capacity of bridge wall at TREFBW
DCPBW	Specific heat capacity change per degree of bridge wall
TREFBW	Reference temperature for RHOBW, LAMBW, CPBW of separation wall (relevant for FDATABW = 2)
FDATAOW	Flag: Property data source and interpolation =1: Constant from specification values RHOOW, LAMOW und CPOW =2: Linear from specification values RHOOW/DRHOOW, LAMOW/DLAMOW und CPOW/DCPOW The values dependent on the outer wall temperature TOW are computed as RHO(TOW) = RHOOW + (TOW - TREFOW)DRHOOW LAM(TOW) = LAMOW + (TOW - TREFOW)DLAMOW CP(TOW) = CPOW + (TOW - TREFOW)DCPOW =3: From characteristic lines CRHOOW, CLAMOW, CCPOW*
RHOOW	Density of outer wall at TREFOW
DRHOOW	Density change per degree of outer wall
LAMOW	Heat conductivity of outer wall at TREFOW
DLAMOW	Heat conductivity change per degree of outer wall
CPOW	Specific heat capacity of outer wall at TREFOW
DCPOW	Specific heat capacity change per degree of outer wall
TREFOW	Reference temperature for RHOOW, LAMOW, CPOW of outer wall (relevant for FDATAOW = 2)
FSPECM	Flag: Handling of system mass of FLUID12 and FLUID34 =1: System mass neglectible =2: System mass considered, outlet equal inlet mass flow =3: System mass considered, outlet different from inlet mass flow
FTTI	Flag: Handling of temperature during time interval 1: Average temperature for time step interval 2: Linear interpolation at each time step
FTSTEPS	Flag: Specification of (sub-) time steps =1: By specification value TISPEP =2: 0.2 of the stable theoretical time increment =3: 0.5 of the stable theoretical time increment =4: 1.0 of the stable theoretical time increment =5: 2.0 of the stable theoretical time increment =6: 5.0 of the stable theoretical time increment
ISUBMAX	Maximum number of time sub steps for initialization
IERRMAX	valign="top" width="558"> Maximum allowed error for initializing step
TISTEP	Time step, always valid while transient calculation
NFLOW	Number of points in flow-direction (max. 100)
NRADBW	Number of radial points in y-direction in bridge wall, (between Fluids, max. 30)
NRADOW	Number of radial points in y-direction in outer wall, (max. 30)
FFREQ	Flag: Frequency of transient calculations =1: At each iteration step =2: At each 2nd iteration step =4: At each 4th iteration step =8: At each 8th iteration step
TMIN	Minimum value of wall temperatures
TMAX	Maximal value of wall temperatures
FSTAMB	Flag: Definition of ambient temperature =0: Definition specification value (TAMB) =1: Defined from superior model (sun)
TAMB	Ambient temperature
ISUN	Index for solar parameter
TIMETOT0	Total time at start of calculation
FRELDIA	=0: heat exchanging area bridge wall AWF13 relates to inner diameter of tube DI =1: heat exchanging area bridge wall AWF13 relates to outer diameter of tube DA
QN	Heat exchanger efficiency (nominal) =Q34
M1N	Primary mass flow(nominal)
M3N	Secondary mass flow(nominal)
V1N	Specific volume for primary inlet (nominal)
V3N	Specific volume for secondary inlet (nominal
P1N	Pressure for primary inlet (nominal)
P3N	Pressure for secondary inlet (nominal)
TM34N	Mean flue gas temperature (nominal) TM34N=(T3N+T4N)/2

The parameters marked in blue are reference quantities for the off-design mode. The actual off-design values refer to these quantities in the equations used.

Generally, all inputs that are visible are required. But, often default values are provided.

For more information on colour of the input fields and their descriptions see Edit Component\Specification values

For more information on design vs. off-design and nominal values see General\Accept Nominal values.

Results

Q21	Transferred heat to primary flow FLUD12 (in steady state cases =QT and Q34, during transient calculations heat flow from separation wall to fluid)
QT	Transferred heat through walls (Please note: while doing transient calculations this result doesn´t make sense anymore)
Q34	Transferred heat from secondary FLUD34 (in steady state cases =QT and Q12, during transient calculations heat flow to the walls)
KA	Overall heat transfer coefficient times area from steady state calculation
DTM	Logarithmic mean temperature difference from steady state calculation
DTLO	Lower terminal temperature difference
DTUP	Upper terminal temperature difference
REFF	Calculated effectiveness (=actual heat transfer/theoretical maximum in case of infinite size)
X2	Steam content (X) at primary outlet
AL12	Calculated heat transfer coefficient FLUID12 to separation wall
AL34	Calculated heat transfer coefficient FLUID34 to outer and separation wall
DP12	Pressure loss primary
DPREF12	Nominal pressure loss primary
DP34	Pressure loss secondary
DPREF34	Nominal pressure loss secondary
VM1	Specific volume of FLUID12 at inlet conditions (nominal)
VM3	Specific volume of FLUID34 at inlet conditions (nominal)
RADAPT	Result ADAPT / EADAPT
M1M1N	Related primary mass flow
M3M3N	Related secondary mass flow
KAKAN	Related kA-value
KAN0	KAN due to KA value
TAVBREND	Mean caloric temperature of the separation wall at the end of the time step
TAVWOEND	Mean caloric temperature of the outer wall at the end of the time step
T2AV	Mean outlet temperature of FLUID12
T4AV	Mean outlet temperature of FLUID34
TX2BEG	Temperature T2 in the beginning of the time step
TX2END	Temperature T2 at the end of the time step
TX4BEG	Temperature T4 in the beginning of the time step
TX4END	Temperature T4 at the end of the time step
QSTO	Heat stored in all walls during time step
QAV12	Mean heat flow from separation wall to FLUID12
QAV34	Mean heat flow from FLUID34 to all other walls
QAVLOSS	Mean heat flow from outer wall to ambient
QENDO	Heat flow from walls to ambient at the end of time step
RALPHO	Heat transfer coefficient to ambient
THBRW	Equivalent thickness of separation wall
THOW	Equivalent thickness of outer wall
REDIA12	Equivalent diameter primary FLUID12
REDIA34	Equivalent diameter secondary FLUID34
MFL12	Mass of FLUIDS12 in primary ducts
MFL34	Mass of FLUIDS34 in secondary ducts
RELQQ	Relaxation theoretical/numerical heat flow
TIMEINT	Total time of the actual time step
TIMETOT	Total time of the simulation
TIMESUB	Integration time of the sub steps
INSFRAC	Fraction of transient calculation steps
ISUB	Number of sub time steps
TISUBREC	Recommended time step
PREC	Precision indicator

Characteristic Lines

In order to set up temperature dependent material properties, three characteristic lines are introduced. All plots showing the temperature on their X-axes:

CRHOBW/CRHOOW: Density of the storage material (*BW = Separation wall, *OW = Outer wall) vs. T
CLAMBW/CLAMOW: Heat conductivity of the storage material vs T
CCPBW/CCPOW: Specific heat capacity of the storage material vs T

All other "characteristic lines" form a circular buffer. The user doesn´t have to take care of them.

CMFL1/CMFL2: Mass of fluid12/fluid34 in differential element of storage dV (not used in every case)/span>
CUFL1/CUFL2: Internal energy of the fluid in differential element of storage dV (not used in every case)
CDAT1/CDAT2: Partial/heat flow between elements of fluid and wall
CHFL1/CHFL2: Enthalpy of the fluids in differential element of storage dV
CTFL1/CTFL2: Temperature of the fluid in differential element of storage dV
CSTAT: Thermodynamical state of the fluids at the lines
CQHIST: History of the heat flows
CTIHIST: History of the time steps

Corresponding to this "characteristic lines", there are also result curves.

RAMFL1/RAMFL2: Mass of fluid12/fluid34 in differential element of storage dV (not used in every case)
RAUFL1/RAUFL2: Internal energy of the fluid in differential element of storage dV (not used in every case)
RADAT1/RADAT2: Partial/heat flow between elements of fluid and wall
RAHFL1/RAHFL2: Enthalpy of the fluids in differential element of storage dV
RATFL1/RATFL2: Temperature of the fluid in differential element of storage dV/span>
RASTAT:< Thermodynamical state of the fluids at the lines
RAQHIST: History of the heat flows
RATIHIST: History of the time steps

Specification matrix MXTSTO and result matrix RXTSTO

The matrix MXTSTO is linked to the output field RXTSTO in the same way as the characteristic curves and result curves mentioned above.

The distribution of the values in the storage and the fluids is stored in both matrices (default matrix MXTSTO for time step t-1 and result matrix RXTSTO for time step t).

For the structure of the matrices, see matrices of component 126.

Physics Used

1 Geometry

In order to handle complex structures of heat exchangers, the storage or pipe masses MWF13 (separation/bridge wall between the two fluids), MWOUT (outer wall of the device), the exchanging area of the separation wall AWF13 and the outer wall AWOUT can be set by the user as well as the length of flow for both of the fluids stored in the variables LSTO12 and LSTO34.

These parameters give a geometric equivalent to wall thickness derived from the geometry of pipes.

Case FRELDIA = 0 (AWF13 related to inner diameter of tube DI)

DI13 = AWF13 / (LSTO12*p) and DIWOUT = AWOUT / (LSTO34*p)

The corresponding "outer diameter" DA can be specified accordingly :

(1)

Case FRELDIA = 1 (AWF13 related to outer diameter of tube DA)

DA = AWF13 / (LSTO12*p)

The corresponding "inner diameter" DI can be specified accordingly :

(1)

Hence this leads to wall thickness using the correlation s = 0.5 * (DA-DI).

In dependency on the switch FVFLUID the volume of the duct can be chosen freely with no respect to the other geometric parameters. On the other hand, it is possible to force a calculation using the pipe geometry.

2.1 Calculation of heat transfer trough the walls of the storage

For a certain conductivity of temperature

(2.1)

and given distances dXnbsp;and dY to the neighbour points, the distribution of temperatures Θ in the walls is calculated by solving the differential equation for all discrete elements in the storage.

(2.2)

simplified to two dimensions the yield is:

(2.3)

Changes to the temperatures starting at an initial state always occur due to heat flow through the walls and the insulating surface (see also chapter 3).

Tip: In order to carry out certain calculations it can be necessary to ignore the outer wall by setting area and mass nearly to zero, while giving a y-resolution only of one element. Insulation can also switched off with suitable values for THISO and LAMISO.

There are 2 algorithms in component 126 for the computation of the wall temperature. Like in comp. 119 for FALGINST=1 the equation (2.3) is solved numerically using Crank-Nicolson-Algorithm . For FALGINST=4 the combined analytic and numeric method is used instead.

2.2 Calculation of the media temperatures

Heat flow between the walls and the fluids depends on position and time, what is described mathematically by linking the convective 2.4 to the conductive terms 2.5:

(2.4)

and

(2.5)

whereas represents the temperature of the wall area facing the fluid. is the temperature of the media and indicates that the direction of the heat flow is orthogonal to the flow direction of the fluid. Heat flow at outer wall will be calculated equivalently.

Heat fluxes at the walls induce a change of the media temperatures, which also influences the whole 1-D grid of the fluid. Gradients orthogonal to the flow direction and the flow dynamics as well will be neglected in order to keep the model simple and save CPU-time. Calculation of time dependent changes of the temperature profile will be done based on mass and energy balances for every volume element.

(2.6)

and

(2.7)

The internal energy of a fluid element is given by , introduced to eqn 2.7 the result is:

(2.8)

Left side of this equation shows the energy stored in the fluids, while the right side gives the resulting energy flows from the walls trough the boundaries. Summing up those terms and the thermal losses gives the change of the internal energy of the walls of the heat exchanger.

(2.9)

Mass of a fluid element is defined by:

(2.10)

All property calculations of the media are based on the EBSILON media library.

2.3 Calculation modes according to FSPECM12 and FSPECM34

FSPECMXX=1: In case of continuous flow Min = Mout conditions and neglectible fluid mass in comparison to the mass of the wall(s), left side of eqn 2.8 is set to zero, what simplifies the following calculation to:

(2.11)

FSPECMXX=2: In case of continuous flow Min = Mout or a zero mass flow Mfluid = 0, there´s no change of the masses in the duct pipe. But if the second condition concerning the mass ratio and coupled to this the energy content of the fluid has to be taken into account, it´s necessary to change eqn 2.8 to the following:

(2.12)

Example: Cooling down a stagnant thermo liquid in duct.

FSPECMXX=3: Fluid mass inside the pipe is variable, what can be the result of changing density as a function of pressure and temperature. In assumption of a constant duct volume different mass flows at inlet and outlet can occur.

Example: Evaporation from a vessel after a pressure drop or temperature jump on the secondary side

2.4 Calculation of the heat flows

The calculation of the heat fluxes is done using eqn 2.8 combined with the settings given by switch FSPEM. In case of neglectible fluid mass the energy balance for both of the fluids appears as following:

The mass of the storage, whose changes of temperature induces a heat flow (Q0(t)), only consists of the wall elements. The fluids are connected thermally via the following equation:

(2.13)

In the same way the calculation of heat losses to the ambient (blue arrows) is carried out and passed to the result values of QAVLOSS and QENDO. The transient storage behaviour is realized by solving the volume integral of all temperature changes:

(2.14)

Balancing all heat flows (according to eqn 2.13) delivers the stored amount of thermal energy with further integration concerning the time step. The result is passed to the variable QSTO:

The balancing of all heat flows (according to Eq.(1)) provides the stored heat quantity with a further integration over the time step, stored in the result variable QSTO:

(2.15)

This value QSTO divided by the interval of the time step Dt shows the mean heat flow QAV12 between separation wall and FLUID12 and also that between separation wall, outer wall and FLUID34 set to result variable QAV34.

Tip: Depended on the magnitude of the temperature gradients and the choice of the time step, it is not possible to get a closed energy balance. If greater miss balances appear, it will be reasonable to reduce the time interval or do a refinement of the time step by adjusting FTSTEPS.

If simulations are done with respect to the fluid mass (FSPECMXX = 2,3), balancing becomes different as shown below:

Left side of eqn 2.8 is not zero anymore, hence fluid mass is considered in this equation. The walls and fluids as well are acting as transient energy storage.

3. Simulation using the EBSILON time series dialogue

The switch FINST generally controls the transient behaviour of the component.

FINST=0: Intervals of the time depended calculation steps are given by the time series dialogue, which takes control of the whole calculation. All transient terms including thermal storages in the equations are going to be solved.

FINST=1: The calculation of the component is steady state, e.g. such a kind of heat exchanger is going to be simulated. Any changes of specifications concerning the heat transfer will result to a new steady state solution for the component. All transient parts of the equations are not considered.

Initializing the simulation using the switch FINIT

FINIT=1: Due to the specifications the heat exchanger is going to be initialized in steady state. In fact that means, a first transient calculation is carried out to lead the system in the state of the long term asymptote. This will be stored to all matrices containing the distribution of temperatures as an initial guess for the following simulations.

Please note:

Specifying the coefficients AL12N and AL34N fixes the overall heat transfer coefficient k shown in eqn 3.1. With all terms forming k are known, the calculation as quite trivial, but other way round it is not possible to get the parts of the sum out of a certain value of k!

(3.1)

In case of this component the heat exchanging area (AWF13) has also to be specified to make the transient calculation work. As a consequence of this, the value kA is fixed, so the steady state and transient part of the simulation get the same input, what is necessary to ensure consistency. Hence design cases which calculate a certain value of kA are not reasonable and therefore this option is not given here.

FINIT=2: Calculations are carried out according to the specifications of the time series dialogue. Results of the previous step generate the input to the next.

Displays

	Form 1		Form 2
	Form 3		Form 4
	Form 5		Form 6
	Form 7		Form 8
	Form 9		Form 10
	Form 11		Form 12
	Form 13		Form 14

Examples

Click here >> Component 126 Demo 1 << to load example 1 (Economizer with characteristic lines for material properties).

Click here >> Component 126 Demo 2 << to load example 2 (General heat exchanger with losses to ambient).

Click here >> Component 126 Demo 3 << to load example 3 (Super Heater with evaporation).

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