ISRN LUTMDN/TMHP-12/5261-SE
ISSN 0282-1990
A working fluid selection program for
Organic Rankine Cycle
Mikael Olsson
2012
Master Thesis
Department of Energy sciences
Division of Thermal power engineering
Abstract
This thesis handles the problem with fluid selection in organic Rankine cycles application. The main
goal was to write a program that based on user defined variables finds the maximum power output
from a range of fluids.
The program was programmed in Matlab and is coupled with REFPROP that return the fluids
characteristics as enthalpy and entropy etc. The program is preloaded with the fluids found from the
literature review. These fluids were the best to use according to the respective authors. The result is
generated with the main code of the program but using a different solver. The result section consists of
multiple temperatures while the main program is designed to be used with one fix heating and one
cooling temperature. Also a turbine calculation was written to be coupled with the main program.
The results show that superheating have a negative impact on the output power and should be kept as
small as possible. Some fluids however should have some superheating to avoid moisture in the
expansion process. There are three types of fluids that is found: wet, dry and isentropic. The wet fluids
are the ones that should have a degree of superheating as their expansion process otherwise might end
in the wet region of the T-s diagram i.e. moisture at the end.
The cooling has a major impact on the performance. A fluid that’s the best performing with a low
cooling temperature isn’t necessary the best if the cooling temperature is increased.
As the superheating should be kept low the main program uncertain parameter, if the user should
define the pinch-point to the heating media or the amount of superheating, is set to last the mentioned.
ii
iii
Contents
1
2
Introduction ..................................................................................................................................... 1
1.1
Background ............................................................................................................................. 1
1.2
Objective ................................................................................................................................. 1
1.3
Organic fluids properties ......................................................................................................... 2
1.4
Limitations............................................................................................................................... 4
1.5
Acknowledgements ................................................................................................................. 5
Method............................................................................................................................................. 7
2.1
Used ......................................................................................................................................... 7
2.2
Literature review ..................................................................................................................... 7
2.3
ORC Program .......................................................................................................................... 9
2.3.1
Subcritical ...................................................................................................................... 10
2.3.2
Supercritical................................................................................................................... 17
2.3.3
Optimum ........................................................................................................................ 20
2.4
2.4.1
Saturated cycle............................................................................................................... 21
2.4.2
Superheating with no evaporation in the reheater ......................................................... 21
2.4.3
Superheating with evaporation allowed in the reheater ................................................. 21
2.5
3
Tweaked ORC program ......................................................................................................... 21
Turbine .................................................................................................................................. 22
2.5.1
Turbine calculation ........................................................................................................ 22
2.5.2
Stage calculation............................................................................................................ 29
Result ............................................................................................................................................. 35
3.1
Result from the main code..................................................................................................... 35
3.1.1
Saturated ........................................................................................................................ 35
3.1.2
Superheated with no evaporation in reheater ................................................................ 37
3.1.3
Superheating with evaporation allowed in reheater ...................................................... 38
3.1.4
Mass flow superheated and saturated ............................................................................ 40
3.2
The Main Program................................................................................................................. 41
4
Discussion ..................................................................................................................................... 42
5
Conclusion and Future Work ......................................................................................................... 45
6
5.1
Conclusion ............................................................................................................................. 45
5.2
Future work ........................................................................................................................... 45
5.2.1
ORC program ................................................................................................................ 45
5.2.2
Turbine .......................................................................................................................... 45
Program use ................................................................................................................................... 47
6.1.1
Initial screen showing on startup. .................................................................................. 47
iv
6.1.2
Heat source selected ...................................................................................................... 47
6.1.3
Cycle properties selected ............................................................................................... 48
6.1.4
Component Data ............................................................................................................ 49
6.1.5
Substances ..................................................................................................................... 50
6.1.6
Cooling .......................................................................................................................... 50
6.1.7
End result ....................................................................................................................... 51
7
References ..................................................................................................................................... 55
8
Appendix A.................................................................................................................................... 57
9
8.1
ORC Program ........................................................................................................................ 57
8.2
Heat source files .................................................................................................................. 104
Appendix B.................................................................................................................................. 106
9.1
Turbine ................................................................................................................................ 106
9.2
Turbine calculation .............................................................................................................. 123
9.3
Stage calculation.................................................................................................................. 127
10
Appendix C.............................................................................................................................. 132
10.1
How to connect REFPROP to MATLAB ............................................................................ 132
v
Nomenclature
A
a
b
c
cN, cr
cp
Cp
Cp
cv
h
m
M
P
ploss
Q
q
R
r
Re
s
T, t
U
v
w
Ytot
Annular area
Velocity of sound
Axial chord
Absolute velocity
Blade chord
Constant pressure specific heat
Diffuser pressure recovery coefficient
Diffuser Pressure recovery coefficient
Constant volume specific heat
Enthalpy
Mass flow
Molar weight
Pressure
Pressure loss
Heat
Dynamic pressure, specific heat
Specific gas constant
Radius, reaction
Reynolds number
Entropy
Temperature
Blade speed
Absolute velocity
Relative velocity
Total loss coefficient
Greek
α
β
ε
η
θ
λ
μ
ν
ρ
ϕ
ψ
Absolute flow angle
Relative flow angle
Efficiency heat exchanger
Isentropic efficiency
Stagger angle
Stage load coefficient
Axial velocity ratio
Specific volume, Blade speed ratio
Density
Stage flow coefficient
Stage load coefficient
vi
Subscript
0
1
2
3
4
5
6
7
8
9
cool
high
hub
low
m
N
p
r
s
SPVH
t
tip
VPPH
Total states
Nozzle entry. State after condenser
Nozzle exit and rotor inlet. State after pump
Rotor exit. State after reheater pump pressure
side.
State before turbine
State after turbine
Condensation state
State after preheater
State after evaporator
State after reheater condenser pressure side
Cooling media
Heat source inlet
Blade hub
Heat source outlet
Mean value
Nozzle
Pump
Rotor
isentropic
State of heat source between super heater and
evaporator.
turbine
Blade tip
State of heat source between evaporator and
preheater
vii
1
Introduction
1.1 Background
Organic Rankine cycles are becoming more and more interesting as the need for energy conservation
is increasing. An ORC can be used to produce electrical power from low-grade heat like industrial
waste heat, geothermal water and solar. The major part of the world’s electricity is produced with
fossil fuels [1] and a large part of the energy is wasted. Quoilin et al. [2] even states that as much as
50 % of heat generated in industry is waste heat, i.e. the potential of energy recovery is vast.
Many reports have been published on the subject of optimal fluids to be used in an ORC. The
conditions for these “optimum” fluids differs which makes the results hard to overview. Also the
screening process of fluids differs from the reports, as some screens for high critical temperature while
others screen for low environmental impact.
A program is needed for calculation of electrical power output, available from a heat source where the
working fluid(s) can be chosen and find the optimum pressure and medium for highest power output.
1.2 Objective
There is no such thing as an optimum fluid to use in ORC and there is therefore much confusion in
what to choose as working fluid. Many reports show an optimum fluid under their respective
conditions thus stating that the other fluids perform worse. However with a decrease or increase of
temperature the optimal fluid could change as some of the other fluids might perform better. Also
many reports do not focus on what could be produced from a given heat source but instead decides a
power output and finds what heat is needed.
The goal of this Master thesis work is to write a program that with a given temperature and mass flow
of an heat source, oil or water, calculate what fluid and pressure from user defined parameters that
gives the highest power output. The user defined parameters that will be set by the user is:










What heat source, water or oil.
Temperature and mass flow of the heat source
If water is used, then the pressure of this must be set
Pressures, between which pressures is the program going to search between and what interval
If the fluid should be superheated when running subcritical cycle.
Isentropic efficiencies of pump and turbine
Which fluids the program is going to try
Cooling, air or water. User can choose to specify the inlet temperature or use a default value.
Ambient temperature
Pinch-points for condenser and preheater, pressure drop heat exchangers, efficiency of
reheater and temperature rise of the cooling media during the condensation. All of these have
default values that can be loaded by the user.
The program has been written in MATLAB and has a graphical interface to make it easier for the user.
1
The program is also tweaked to do an analysis of the ambient temperature effect on the performance of
the cycle for different heating temperatures with two mediums. The result of this will be presented in
section 5.
A turbine program was also created to enable the user to do a turbine calculation if wanted. The
turbine will not be a part of the result.
1.3 Organic fluids properties
From the normal steam cycle we know the look of the saturation curve of water in the T-s diagram.
Organic fluids (and refrigerants) however can have a different kind of curves. The different mediums
can be characterized based on three different curves that occur and can be seen in figures 1-3.
The bell-shaped curve, or b-cycle [3], as seen in figure 1 is familiar from waters saturation curve. The
slope is positive on the liquid side and negative on the vapour side. With the negative slope of the
curve and without superheating the expansion often ends somewhere in the moist region and therefore
fluids of this type is referred to as wet fluids.
Figure 1: The b-cycle or the wet fluids T-s
diagram
Figure 2: The o-cycle or the dry fluids T-s
diagram.
Figure 3: The isentropic fluids T-s diagram
2
The overhanging shape, the o-cycle, can be seen in figure 2. The fluids of this type is often referred to
as dry fluids because the positive slope on the vapour side makes moisture in the end of expansion
almost impossible because it’s still in the superheated area. Only very small expansions from a high
pressure or expansion to very small pressures might result in moisture.
The last shape is found for isentropic fluids and is seen in figure 3. The vapour side slope is infinitely
large and therefore the fluids of this type have the same advantage as the dry, no moisture in or after
the expansion. The fact that the expansion process never is isentropic will result in that the end of
expansion is superheated. Isentropic is actually an idealized view as many isentropic fluids could be
classed as a dry fluid.
The saturation curves can also be shown by Troutons rule. With a known boiling temperature and
enthalpy of vaporization the entropy of vaporization follows the simple rule of [4]:
∆𝑆𝑣𝑎𝑝 (𝑇𝑏 ) =
∆𝐻𝑣𝑎𝑝 (𝑇𝑏 )
𝑇𝑏
𝐽
≈ 88 𝑚𝑜𝑙·𝐾
Where the value 88 is when the boiling temperature is at the pressure 1 bar.
The result is not always correct as its accuracy are reduced when there’s hydrogen bonds although it
gives a good approximation.
The number of fluids that could be used is many, and the suitability of one fluid depends on numerous
of things. Firstly one must consider the location of the power plant in the event of a leak. If it’s located
in the vicinity of populated area, more flammable and toxic fluids might be exchanged for less
hazardous mediums. Secondly the environmental aspect has to be considered, e.g., what global
warming potential has the fluid. Lastly the economical part has to be weighted in. The best performing
fluid might not be the best economically. The program does not account for these important parts
because the application may differ and the user has to decide what’s acceptable concerning economics,
risks and environment.
Figure 4 show how the properties of three fluids from the same “family” changes in T-s diagram with a
fix evaporation and condenser temperature that’s been set to 100 °C and 20 °C respectively. Note that
the figure have been tampered with because different reference states is used for each fluid but the
temperature and entropy difference between two points in the curve is still the same. The figure shows
that three fluids that are very alike have different properties.
3
Figure 4: T-s diagram of butane, pentane and hexane showing increase of the overhanging shape
the bigger the molecule gets. P = pressure in bar and T= temperature in Kelvin.
1.4 Limitations
Autoignition is mentioned but not taken into account for the fluids. The user needs to be aware of this
when selecting fluids along with other risks when leakage might occur as ignition sources and toxicity
etc.
The heat exchanger areas is not studied and this can somewhat tip the scale in some fluids favor.
No economic study is made. A fluid that’s have the best thermo dynamical performance might not be
the best investment due to component size, i.e. an economic optimum could be found where
component size are smaller with lower thermo dynamical performance.
Only pure fluids are considered.
The fluids that are run are pre-selected by screening of literature.
REFPROP is a program that calculated the fluids properties and there are some uncertainties in the
values. Depending on what parameter or fluid it calculates this uncertainty is ranging from between 0
to 2 % fault from the correct value.
The main program can only handle one heating temperature and one cooling temperature so the
tweaked program needs to be adjusted. However no major changes needs to be made because the main
code is still used. The difference is that the main program only search for maximum value from a list
of pressure and fluids while the tweaked program collects the maximum values for many
temperatures. It’s this way because the program is intended to only find one fluid and pressure from a
range of values.
The fluids vapor states are assumed to be ideal gases for the turbine calculations so the ideal gas rules
can be applied.
4
1.5 Acknowledgements
I would like to thank the department of thermal power engineering for allowing me to do this master
thesis. A special thanks goes out to Marcus Thern, Magnus Genrup and Björn Nyberg for guiding me
through the times when I saw the light at the end of the tunnel and it turned out to be a train.
I would also give thanks to the coffee machine at the department of energy sciences for giving me the
energy to start working in the mornings.
5
6
2 Method
This chapter presents the methods and calculations made in the thesis
2.1 Used
The aim of this work has been to investigate how different fluids affect the thermodynamic
performance of an organic Rankine cycle. The organic Rankine cycle was studied with a program
developed in MATLAB. The program makes it possible to do thermodynamic evaluation of the
Rankine cycle. The program is divided into two different parts, the main program and the graphical
user interface (GUI) in one file while the heat mediums have been put in separate files.
The program has the option of using different physical fluids and the fluids properties is made
available by a program called REFPROP [5]. REFPROP is called as a subroutine from inside
MATLAB. REFPROP return one or more values given two input values (e.g. enthalpy and entropy as
input values give temperature, pressure etc.).
The programs graphical interface (GUI) is built up using MATLABs built in function guide. Guide is a
click and drag interface that enables the user to, after defining size of the window, drag edit boxes, text
boxes, check boxes etc. and generates the code needed to later access and program what the item is
supposed to do.
Turbine is programmed in MATLAB with the help of the loss program AMDC-KO-MK (Ainley
Mathieson et al. loss model) that’s already been programmed and in use by LUAX-T.
2.2 Literature review
Several authors have studied the organic Rankine cycle but the studies made on the influence of the
working fluids on performance can differ. Most studies have a screening process of some sort where
the authors selected fluids that fulfilled their criteria’s. Some studies screened with safety and
environmental aspects as criteria where others screened based on critical temperatures or size of the
components. The temperature range also differed for the studies. The literature review identified the
fluids in table 1 that where suggested by the respective authors. One fluid, R24fa was recommended
but has been disregarded as it’s not found in the REFPROP database.
A few of the fluids were recommended by more than one source. The different studies have been made
for applications with power output ranging from a few kW using solar energy up to MW class with
high temperature geothermal heat source.
7
Table 1: Optimum fluids from papers written on the subject.
Medium
Ref
R114
[6]
R245fa
[6]
R123
[6], [7]
iso-pentane
[6]
n-pentane
[6] [8]
R141b
[6]
R113
[6], [9]
R227ea
[10]
cyclopentane [11]
ammonia
[8]
n-butane
[2]
R134a
[12]
Table 2 show some reference values of the fluids. The column REFPROP TPFLSH shows the
maximum temperature that can be used in REFPROP for the specific fluid. Beyond this temperature
REFPROP can’t calculate the fluids properties. If the fluid is called with a temperature higher than this
an error message is displayed and all calculations are stopped. Therefore the limit value of each fluid
has to be added manually so a calculation run of multiple fluids and temperatures don’t stop because
the limitation is reached.
Column “type of fluid” shows the classification of the fluid, with definitions from section 3.3. As
stated in that section there are three kinds of fluids, wet, dry and isentropic. The isentropic fluid shape
as shown in figure 3 is rarely found because it’s merely an idealization. The isentropic fluids often
have the tendency of an overhanging shape, i.e. dry and are therefore sometimes referred to as dry.
Table 2: Highest temperature on the working fluids that REFPROP handles, type of fluid and
the critical pressure and temperature.
Medium
R245fa
R134a
R227ea
iso-pentane
R141b
R114
R113
n-butane
R123
n-pentane
cyclopentane
ammonia
REFPROP
TPFLSH (°C)
167
182
202
227
227
234
252
302
326
327
327
427
Type of fluid
Critical pressure
(bar)
Critical
temperature (°C)
Isentropic/dry
wet
dry
dry
Isentropic/dry
Isentropic/dry
Isentropic/dry
Isentropic/dry
Isentropic/dry
dry
dry
wet
36.5
40.6
29.2
33.8
42.2
32.6
33.9
37.96
36.6
33.7
45.15
113.33
154
101
101.7
187.2
204.3
145.7
214.06
152
183.6
196.5
238.5
132.2
8
2.3 ORC Program
Program is split up into two parts, subcritical and supercritical cycles. The user needs not choose what
cycle to run, the program chooses based on the pressure. The structure can be seen in figure 5 and is
explained briefly below. The subcritical and supercritical calculations are presented in detail in section
4.3.1 and 4.3.2 respectively.
The user specifies values that the selection is based on. Values that need to be provided are listed in the
objectives. The fluids available are predetermined from section 4.2 and the user selects which of these
fluids to run.
The program starts with the first fluid and the starting pressure and chooses what cycle to run. If all the
pressures in the range are below the condenser pressure the program starts with the next fluid. After
every cycle calculation that is done all values are stored and the next pressure in the range starts. When
all the pressures are done the program continues to the next fluid.
When all fluids have been calculated the selection takes place. The program searches for the largest
value of either efficiency or power output depending on what’s been selected. When this is finished the
result of the fluid with the highest value is displayed.
9
User specified
values
All pressures
lower than
condenser
pressure
Fluids
Pressure range
P>Pc
T>Tc
P<Pc
Supercritical
Subcritical
Store results
All pressures done
Next pressure
All fluids done
Find maximum
Maximum
power
Maximum
efficiency
Display result
Display result
Figure 5: Calculation procedure of the ORC program where the super- and sub-critical are two
different calculation routines chosen based on the pressure (P=pressure).
2.3.1 Subcritical
Figure 6 shows where the following state points are. The order they are presented is in the sequence
the program works.
10
Figure 6: View of components in the subcritical cycle. SH = super heater, VP = evaporator, PH =
preheater. Turbine between state 4 and 5, pump between 1 and 2. Reheater is located between 2
and 3 (and 5 to 9) and the condenser between state 9 to 1. Inlet heat source is at high_heat and
the outlet at low_heat. Numbered states are for the working fluid and the named states are for
the heat source and cooling medium.
2.3.1.1 State 1
State 1 is located just after the condenser and at this point the fluid is completely condensed. It is
assumed that the level of cooling is pre-determined before the study continues. This means that the
temperature of the incoming cooling media and the temperature rise of the condensation phase (state 6
to 1) is known. The pinch-point of the condenser, i.e. the size of it, is assumed to be known. As the
temperature is constant over the condensation phase the fluid temperature at state 1, after
condensation, is set by the cooling media inlet temperature, the condenser pinch-point and the
temperature rise of the cooling media during the condensation phase. Temperature t1 is equal to t6.
𝑡1 = 𝑡6 = 𝑡𝑖𝑛_𝑐𝑜𝑜𝑙 + 𝑝𝑖𝑛𝑐ℎ𝑐𝑜𝑛𝑑 + 𝑡𝑒𝑚𝑝_𝑟𝑖𝑠𝑒𝑐𝑜𝑜𝑙
(2.3.1.1)
With the temperature known the condenser pressure can be calculated with REFPROP because point 1
lies on the saturation curve as saturated liquid (state 6 as saturated vapour). The thermodynamic state
is thus completely determined and the condenser pressure is calculated with REFPROP with the
temperature and saturated liquid.
A condition has been set that the condenser pressure must be 10 kPa or higher. If the pressure is larger
than 10 kPa enthalpy and entropy is returned by using the pressure and state of saturated liquid as
input. If the pressure has been forced to 10 kPa the enthalpy and entropy is returned using pressure and
temperature as input instead. Often this isn’t a problem but for fluid with high critical temperature (and
low critical pressure) this problem could occur. Temperature instead of saturated liquid value isn’t
used as input value from the beginning because REFPROP might have problems separating the liquid
values from the vapour values when on the saturation curve.
11
2.3.1.2 State 2
Pressure at state 2, after the pump, is defined by the user and can be a range of values that’s to be
tested. The condition to continue is that the pump pressure is larger than the condenser pressure
otherwise the program tests the next pressure, if the user has defined more than one. If the pressures
given don’t work for a fluid the program continues to the next fluid if more than one has been selected.
If the pressure condition fails for all fluids an error message is returned.
The isentropic efficiency of a pump can be expressed as:
𝜂𝑝 =
ℎ2𝑠 −ℎ1
ℎ2 −ℎ1
(4.3.1.2)
h2s, isentropic enthalpy, is calculated with the pump pressure and entropy of state 1. By using
eq. 2.3.1.2 h2 can now be calculated because the efficiency is defined by the user. As the pressure is
known the temperature t2 and entropy s2 can be returned from REFPROP.
2.3.1.3 State 7
State 7 is after the preheater (PH) i.e. the fluid is in the state of saturated liquid. However a condition
needs to be fulfilled, the saturation temperature must not exceed the inlet temperature of the heat
carrier. In case this happens the program goes to the next fluid if more than one has been selected.
All properties can be found by using pressure and the fact that this state is saturated liquid. However,
the pressure is lower than that in state 2 because pressure drops occur in the reheater (state 2=>3) and
preheater. The pressure drop (ploss) is predefined as 5% in each heat exchanger but this can be changed
by the user by not checking the box “use default values” and entering a value. The pressure drop is
denoted ploss. The pressure becomes:
𝑃7 = 𝑃3 · (1 − 𝑝𝑙𝑜𝑠𝑠 )
(2.3.1.3)
2.3.1.4 State 8
This state is after the evaporator (VP) and the fluid is in the state of saturated vapour. With the
pressure drop accounted for the properties can be found with the pressure and state of saturated
vapour. Note that the temperature, t8, will be lower than t7 because the pressure, P8, is lower than P7 if
pressure drop is greater than nought. The fluid passed three heat exchangers i.e. the exponent becomes
3.
𝑃8 = 𝑃7 ∙ (1 − 𝑝𝑙𝑜𝑠𝑠 )
(2.3.1.4)
2.3.1.5 State 4
State 4 properties depends if the user selected superheating or not. If the superheating value is set to
nought, state 4 becomes state 8 (saturated vapour) and the super heater is removed. If the user sets it to
a value greater than nought then:
𝑡4 = 𝑡8 + 𝑢𝑠𝑒𝑟 𝑠𝑝𝑒𝑐𝑖𝑓𝑖𝑒𝑑 𝑣𝑎𝑙𝑢𝑒
(2.3.1.5)
𝑃4 = 𝑃8 ∙ (1 − 𝑝𝑙𝑜𝑠𝑠 )
(2.3.1.6)
12
A control is made that the temperature t4 isn’t higher than the heat source for the specific pressure. If
the temperature is too high it stops for that pressure and moves on to the next fluid. If it passes, the
program continues.
With t4 and P4 known the enthalpy and entropy of state 4 is found.
2.3.1.6 State 5
State 5 is after the expansion through the turbine. The isentropic efficiency a turbine is expressed as:
ℎ −ℎ
𝜂𝑡 = ℎ 4−ℎ 5
4
5𝑠
(2.3.1.7)
Pressure at turbine outlet is the same as condenser pressure. Isentropic expansion, i.e. s5=s4, and
pressure gives h5s. Using eq. 2.3.1.7, h5 is calculated. Pressure and enthalpy gives temperature and
entropy.
Figure 7: The subcritical process for a dry fluid with isentropic pump and turbine work shown
in a T-s diagram. The numbered states correspond to the ones in figure 6.
Before continuing a check needs to be made of where state 5 lies in the T-s diagram, see figure 7. If
state 5 is in the moist region or on the saturation curve a reheater can’t be used and state 9 and 3 is
skipped and leaves state 6 equal to state 5. If the reheater is removed the program restarts the
calculation beginning with state 2 with one less heat exchanger, i.e. the states 7,8 and 4 will now
experience one less pressure drop.
State 3 and 9 only exist if a reheater is used.
2.3.1.7 State 6
State 6 is always saturated and is located inside the condenser as saturated vapour when the end of
expansion is superheated. If the expansion end in the moist region state 6 is equal to state 5.
13
2.3.1.8 State 9
State 9 position in the above T-s diagram is dependent of the reheater efficiency. Low reheater
efficiency brings state 9 closer to state 5 while with a higher efficiency closer to state 6. Heat
exchanger efficiency is defined as [13]:
𝜀 = 𝑄̇
𝑄̇
𝑚𝑎𝑥
(2.3.1.8)
The maximal transferrable heat is from state 5 down to the temperature at state 2, i.e. state 9 can never
be as low as state 6.
𝑄̇𝑚𝑎𝑥 = 𝑚̇ ∙ (ℎ5 − ℎ@𝑡2,𝑃𝑐𝑜𝑛𝑑 )
(2.3.1.9)
The mass flow is constant and eq. 4.3.1.8 then gives:
𝜀=ℎ
ℎ5 −ℎ9
5 −ℎ@𝑡2,𝑃_𝑐𝑜𝑛𝑑
(2.3.1.10)
h5 known, h@t2,P_cond is returned by REFPROP and with the efficiency set by user enthalpy, h9 is
calculated. Condenser pressure and h9 gives the temperature and entropy of state 9.
2.3.1.9 State 3
State 3 is depending on state 9, and therefore on the reheater efficiency. Its upper limitation is the
temperature of state 5. With an energy balance h3 is calculated and its dependency of state 9 can be
seen as state 2 and 5 are fix.
𝑚̇ ∙ (ℎ3 − ℎ2 ) = 𝑚̇ ∙ (ℎ5 − ℎ9 )
(2.3.1.11)
Pressure is:
𝑃3 = 𝑃2 ∙ (1 − 𝑝𝑙𝑜𝑠𝑠 )
(2.3.1.12)
In eq. 2.3.1.4, mass flows are the same and 2.3.1.4 can be written as:
ℎ3 = (ℎ5 − ℎ9 ) + ℎ2
(2.3.1.13)
Enthalpy h3 and pressure P3 gives temperature and entropy.
2.3.1.10 Heat source and working fluid mass flow
Temperature of the heat source media is calculated using the temperature at state 7 and adding the
pinch-point of the preheater like this:
𝑡𝑉𝑃𝑃𝐻 = 𝑡7 + 𝑝𝑖𝑛𝑐ℎ𝑝𝑟𝑒ℎ𝑒𝑎𝑡𝑒𝑟
(2.3.1.14)
Mass flow of the fluid is calculated by a heat balance over the vaporizer and super heater, see figure 8.
𝑚̇ℎ𝑒𝑎𝑡 ∙ (ℎℎ𝑖𝑔ℎ − ℎ𝑉𝑃𝑃𝐻 ) = 𝑚̇ ∙ (ℎ4 − ℎ7 )
(2.3.1.15)
Rearranging eq. 2.3.1.15 gives:
14
𝑚̇ =
𝑚̇ℎ𝑒𝑎𝑡 ∙(ℎℎ𝑖𝑔ℎ_𝑖𝑛 −ℎ𝑉𝑃𝑃𝐻 )
(2.3.1.16)
(ℎ4 −ℎ7 )
Figure 8: Heat balance over the super heater and evaporator.
The method of calculating hhigh_in-hVPHP depends on what heating media is being used. REFPROP is
used when water is selected. Temperature thigh and pressure set by user and tVPPH known gives
hhigh-hVPHP.
When using oil things get a little more complicated. Different thermal oils have different thermal
properties. Instead of using a specific oil the specific heat is approximated using [14]:
𝑐𝑝 = (
𝐴
√𝜌
𝐽
]
𝑔℃
+ 𝐵 ∙ (𝑡 − 15)) · 4186 [
(2.3.1.17)
Where A and B are factors depending on the type of oil, ρ density at 15 ºC and t the temperature. The
factors A and B are set to 0.415 and 0.0009 respectively (petroleum oils) [14]. Density has been set to
870 kg/m3. This value has been chosen because the density of many thermal oils seems to be in the
area of 850-900 kg/m³.
Enthalpy is a function of temperature and pressure.
Therfore:
𝜕ℎ
𝜕ℎ
𝑑ℎ = 𝜕𝑇 | 𝑑𝑇 + 𝜕𝑃| 𝑑𝑃
𝑃
𝑇
(2.3.1.18)
Last term is nought and therefore the specific heat can be expressed as:
𝜕ℎ
𝜕𝑇 𝑃
𝑐𝑝 = ( )
(2.3.1.19)
This together with eq. 3.3.1.7 gives the enthalpy difference (general notation):
𝑇
ℎ2 − ℎ1 = ∫𝑇 2 𝑐𝑝 (𝑇)𝑑𝑇 =
1
𝐴
√𝜌
∙ (𝑇2 − 𝑇1 ) + 𝐵 ∙
(𝑇22 −𝑇12 )
2
+ 15 ∙ (𝑇1 − 𝑇2 )
Temperatures thigh and tVPPH known gives the enthalpy difference from eq. 2.3.1.20.
15
(2.3.1.20)
Outlet temperature on the heating side, tlow is calculated from a heat balance around the whole heating
side and using eq. 2.3.1.20 or REFPROP, depending on if oil or water are used. Outlet temperature is
iterated based on the heat. Transferred heat is known and by using eq. 2.3.1.20 for oil and REFPROP
for water the temperature can be found by using the Newton-Raphson method:
𝑥𝑛+1 = 𝑥𝑛 −
𝑓(𝑥𝑛 )−𝑓(𝑥𝑛+1 )
𝑓′(𝑥𝑛 )
(2.3.1.21)
Figure 9: The Newton-Raphson method. Blue line is the function and the red lines the tangents.
x1 is the initial guess.
The method is a quick way of finding the solution. Based on an initial guess the method is reducing
the error for every new guess until convergence as seen in figure 9. The program employs this method
as:
𝑒𝑟𝑟𝑜𝑟
𝑛)
𝑡𝑛+1 = 𝑡𝑛 − 𝑅𝐿𝑋 ∙ 𝑓′(𝑡
(2.3.1.22)
Error is the difference of known and calculated transferred heat. RLX is a relaxation factor between 0
and 1to make the iteration more stable. t is in this case the outlet temperature and the slope f’(tn) is cp.
A problem that may arise is that the outlet temperature is lower than the temperature at state 3.
Therefore a condition is that the outlet temperature always is at least 5°C higher than in state 3. If this
isn’t fulfilled the pinch-point is increased by one degree at a time until the condition is fulfilled.
Therefore the mass flow and temperatures above is nested into this loop.
2.3.1.11 Cooling
The cooling is divided into two parts, the condensation and the cooling down to condensation
temperature. User has the choice of water or air cooling. The energy removed between state 6 and
state 1 (condensation) is calculated with a energy balance over the condensation phase:
𝑚̇ ∙ (ℎ6 − ℎ1 ) = 𝑚̇𝑐𝑜𝑜𝑙 ∙ (ℎ𝑐𝑜𝑜𝑙𝑖𝑛 − ℎ𝑐𝑜𝑜𝑙𝑐𝑜𝑛𝑑 )
(2.3.1.23)
16
The temperature at tcool_cond is fully decided by the user with the inputs of inlet temperature and
temperature rise and tcool_in is the inlet temperature. REFPROP with pressure and temperature as input
variables together with eq. 4.3.1.22 gives the mass flow of the coolant. Pressure for water is set to 5
bar and air is set to atmospheric (1 bar).
A heat balance over the condenser results in:
𝑚̇𝑐𝑜𝑜𝑙 ∙ (ℎ𝑐𝑜𝑜𝑙𝑜𝑢𝑡 − ℎ𝑐𝑜𝑜𝑙𝑖𝑛 ) = 𝑚̇ ∙ (ℎ9 − ℎ1 )
(2.3.1.24)
Eq. 2.3.1.24 returns hcool_out and with this as input together with pressure, the temperature t cool_out is
returned from REFPROP.
2.3.1.12 Super heater-vaporizer heat side
A heat balance around the super heater gives that the transferred heat is known. With this, the same
procedure as for tlow is used i.e. using eq. 2.3.1.20 or REFPROP depending on if oil or water is used
and then iterates the temperature based on the known transferred heat.
2.3.1.13 Performance subcritical cycle
Following equations give the performance of the cycle:
𝑊𝑜𝑢𝑡 = 𝑚̇ ∙ (ℎ4 − ℎ5 )
(2.3.1.25)
𝑊𝑖𝑛 = 𝑚̇ ∙ (ℎ2 − ℎ1 )
(2.3.1.26)
𝑄𝑖𝑛 = 𝑚̇ ∙ (ℎ4 − ℎ3 )
(2.3.1.27)
The maximum transferable heat from the heat source is:
𝑄ℎ𝑒𝑎𝑡_𝑠𝑜𝑢𝑟𝑐𝑒 = 𝑚̇ℎ𝑒𝑎𝑡 · (ℎℎ𝑖𝑔ℎ𝑖𝑛 − ℎ@𝑡𝑎𝑚𝑏𝑖𝑒𝑛𝑡 )
(2.3.1.28)
The efficiency can be calculated in two different ways, cycle efficiency (eq. 2.3.1.29) or the total
efficiency (eq. 2.3.1.30)
𝜂𝑜𝑟𝑐 =
𝑊𝑜𝑢𝑡 −𝑊𝑖𝑛
𝑄𝑖𝑛
𝑊𝑜𝑢𝑡 −𝑊𝑖𝑛
𝜂𝑡ℎ = 𝑄
ℎ𝑒𝑎𝑡_𝑠𝑜𝑢𝑟𝑐𝑒
(2.3.1.29)
(2.3.1.30)
Eq. 4.3.1.29 describes how well the fluid performs in the cycle while eq. 4.3.1.30 describes how well
the fluid utilize the given heat source.
2.3.2 Supercritical
Figure 10 shows the supercritical cycle and is modelled up in very much the same way as the
subcritical. The biggest difference is that instead of using three heat exchangers (PH, VP, SH) it only
uses one on the heating side. The state 9 is continued to be called 9 even though state 7 and 8 don’t
exist to make it easier to translate the subcritical to supercritical cycle.
17
Figure 10: Schematic view of the components in the supercritical cycle. Turbine, reheater,
condenser and pump unchanged. Only one heat exchanger needed.
The program chooses if its runs sub- or supercritical or cycle for each selected fluid based on the
pressure. If the pressure after the heat exchanger is greater than critical pressure of the fluid it runs the
supercritical cycle. However a temperature condition must also be fulfilled to make it work. The
critical temperature plus a pinch-point needs to be lower than the inlet temperature of the heat media.
This pinch-point has been set to 25 °C.
The temperature at state 4 is set to the heating media inlet temperature minus the pinch-point of 25 °C.
REFPROP then gives the enthalpy and entropy of this state. Otherwise state 1,2,3,5,6 and 9 is
calculated in the same way as for subcritical.
The mass flow for the fluid and the outlet temperature of the heating media calculation differs from the
subcritical cycle. Inside the heat exchanger a pinch point is set by the user (not to be confused with the
previous pinch that decided state 4). The pinch-point takes the same value that the user defines for the
preheater in subcritical. Instead of the describing the temperature difference of the fluid and heating
media after the preheater the pinch is now the minimum difference between the two mediums
somewhere inside the heat exchanger, see figure 11 as an example. The mass flow of the fluid is
iterated by searching, point by point, for the temperature difference using eq. 4.3.1.19 for oil or
REFPROP for water and the Newton-Raphson method as described earlier.
The temperature and mass flow dependency on each other can be hard to show. The following
equations are used to show this.
𝑚̇ =
𝑚̇ℎ𝑒𝑎𝑡 ∙(ℎℎ𝑖𝑔ℎ_ℎ𝑒𝑎𝑡 −ℎ𝑙𝑜𝑤_ℎ𝑒𝑎𝑡 )
(ℎ4 −ℎ3 )
(2.3.2.1)
18
The mass flow is dependent on outlet temperature of the heat source. The outlet temperature however
is dependent on where the pinch point lies.
𝑄𝑓𝑙𝑢𝑖𝑑 = 𝑚̇ ∗ (ℎ4 − ℎ@𝑝𝑜𝑖𝑛𝑡 𝑜𝑓 𝑖𝑛𝑡𝑒𝑟𝑒𝑠𝑡 )
(2.3.2.2)
𝑄ℎ𝑒𝑎𝑡 = 𝑄𝑓𝑙𝑢𝑖𝑑
(2.3.2.3)
The outlet temperature is therefore a function of the mass flow while the mass flow is a function of the
temperature.
The number of points it runs varies with the enthalpy difference between state 3 and 4. Each point is
100 J/kg apart. E.g. if starting point is state 3 the next point (point 2) is 100 J/kg larger than that, point
3 is 200 J/kg larger than point 1 etc. until state 4 is reached. The iteration result in the fluid mass flow
and the outlet temperature of the heat source as the mass flow and temperature
are depending on each other.
Figure 11: An example of the T-Q diagram for supercritical cycle. The green vertical line shows
the smallest difference between the heat source (red) and working fluid (blue). The smallest
difference is the pinch point.
19
The advantage of the supercritical can be seen by comparing the T-Q diagrams of a subcritical
(figure 12) and a supercritical (figure 11) cycle. The area between the working fluid and heat source is
a loss, i.e. it should be as small as possible. The subcritical has a limitation with the evaporation
process taking a large portion of the energy available. The end of evaporation will always have a larger
temperature difference to the heat source than after the preheater with a loss that not can be reduced
for the evaporator. With superheating the loss after the evaporation phase is reduced. The supercritical
do not have any phase change and therefore the area between the fluid and heat source can be reduced.
Figure 12: A sketch of a T-Q diagram of a subcritical cycle. The heat source is the top line and
the working fluid is the one below. The pinch point is at the “notch” between PH (preheater) and
VP (evaporator) encircled in the figure.
2.3.3 Optimum
All state points and performance data has their respective values stored in matrixes. Depending on
what the user is searching for, power or efficiency, the maximum value is found and returns the row
and column for that value, i.e. pressure and media. With these, all the values are collected so that the
T-s and T-Q diagrams can be plotted.
By searching the maximum efficiency or work output matrixes the row and column of the highest
value is returned. With the row and column numbers the following values of interest are collected and
displayed:










What fluid was best
Sub- or supercritical cycle
Pressure
Power output
Mass flow
Cycle and total efficiency
Temperature of the heat source outlet
Temperature of the cooling outlet
If the pinch needed to be moved the new pinch are displayed
The T-s and T-Q diagrams with the cycle plotted.
20
2.4 Tweaked ORC program
The tweaked program uses the same calculation procedure as the program in section 4.3. The
difference is that the cooling and heating temperatures can be varied. This is to investigate the
temperature impact on the cycle for two fluids. Three different cases are made and are presented
below. The cooling temperature only affect the condenser pressure and therefore how long the
expansion is while the heating temperature affect the reheater and preheater depending on which case
is run. All the conditions set in section 4.3 is still active on top off the new in each case.
2.4.1 Saturated cycle
The highest cycle temperature (t4) is limited to the saturation temperature, i.e. no super heating. This
makes the cycle temperature independent on how high the heating temperature is, but the fluid
temperature must still be lower than the heating temperature. As it only running the saturated cycle no
super heater is used.
2.4.2 Superheating with no evaporation in the reheater
The highest cycle temperature (t4) follows the heating temperature with a pinch of 10 °C. This means
that at some point the fluids is going to be superheated. If the temperature becomes high enough there
can be enough energy to do all of the preheating in the reheater. In this case this isn’t allowed and
therefore the reheater efficiency is lowered (removed when the efficiency reaches nought) until the
preheater is still needed. All evaporation is made in the evaporator.
2.4.3 Superheating with evaporation allowed in the reheater
The highest temperature is set as in 4.4.2. This case however allows evaporation in the reheater. This
means that if there’s enough energy the preheater is removed and all the preheating is made in the
reheater. If there’s still energy left the fluid is also allowed to do a part of its evaporation in the
reheater. Therefore all of the evaporation doesn’t necessary take place in the evaporator.
21
2.5 Turbine
2.5.1 Turbine calculation
Figure 13 shows the turbine calculation and is described briefly below.
User defines five design parameters of the turbine. These are stage loading coefficient, reaction, flow
coefficient, mean radius and the rotational speed where the three first is defined as [15]:
𝜓=
Δℎ0
𝑈2
(2.5.1.1)
ℎ −ℎ
𝑟 = ℎ2 −ℎ3
1
𝜙=
𝐶𝑥
𝑈
3
(2.5.1.2)
(2.5.1.3)
The calculation starts with the built in initial guess of one stage. Firstly the flow angles are
determined. Since only one stage has been guessed the last stage calculation starts. The outlet absolute
angle from the rotor is tested at 10 degrees. If the reaction for this value is outside the interval of
0.05<r<0.5 the reaction is set to the corresponding limit value and returns the angles.
The flow coefficient and the blade velocity give the axial velocity through the stage. With angles, axial
velocity and the imported values the stage calculation can be run. The imported values contain the
mass flow and the pressure, enthalpy and entropy before and after the turbine. After this is complete
the static pressure out of the rotor is compared to the pressure calculated from the diffuser. If they
aren’t equal a new stage load is calculated and starts over with the angle calculation. This continues
until the pressures are equal.
If the stage load required is higher than the value the user selected another stage are added and all
calculations are restarted. The flow angles for all but the last stage are calculated with the stage load
and reaction the user selected. This continues and if necessary more stages are added until the stage
load is lower or equal to the user defined value. When this condition is fulfilled the turbine are done.
The described turbine is not to be seen as full out turbine design. The purpose of it is to give the
user an estimation of the turbine performance and geometry, not an actual turbine design.
22
User defined N,
r_m,ψ,ϕ,r and
imported values
One stage guessed, n=1
Flow angles
n-1 stages
Last stage
Stage calculation
Flow angle out
10 or
0.05<r<0.5
P3≠ P3_diffuser,
adjust ψ
ψ_new>ψ
n=n+1
Stage calculation
Pressure before
diffuser,
P3_diffuser
P3=P3_diffuser
ψ_new
ψ_new <= ψ
Result
Figure 13: Calculation procedure of the turbine. P=pressure, n=nr. of stages, ψ=stage loading,
ϕ=stage flow, r=reaction, N=revs per minute and r_m = mean radius.
23
2.5.1.1 Flow angles
Figure 14: Angle definitions according to Schobeiri [16]. Left triangle is after the nozzle and the
right after the rotor. V is absolute and W the relative velocities.
With a program provided by Magnus Genrup, the flow angles can be determined from following
equations [16] with the angles defined as in figure 14:
𝜇2 𝜙 2 (1 − 𝜈 2 ) tan2 𝛼2 + 2 𝜇𝜈𝜙𝜓 tan 𝛼2 − 𝜆2 − 2(1 − 𝑟)𝜆 + (𝜇2 − 1)𝜙 2 = 0
(2.5.1.4)
𝜙 2 (1 − 𝜈 2 )(𝜙 tan2 𝛼3 + 2𝜙𝜆 tan 𝛼3 + 𝜆2 − 2(1 − 𝑟)𝜆𝜈 2 + (𝜇2 − 1)𝜙 2 𝜈 2 = 0
(2.5.1.5)
(1 − 𝜈 2 )(𝜇𝜙 tan 𝛽2 + 𝜈)2 + 2𝜈𝜆(𝜙𝜇 tan 𝛽2 + 𝜈) − 𝜆2 − 2(1 − 𝑟)𝜆 + (𝜇2 − 1)𝜙 2 = 0 (2.5.1.6)
(1 − 𝜈 2 )(𝜙 tan 𝛽3 + 1)2 + 2𝜆(𝜙 tan 𝛽3 + 1) + 𝜆2 − 2(1 − 𝑟)𝜆𝜈 2 + (𝜇2 − 1)𝜙 2 𝜈 2 = 0 (2.5.1.7)
In the equation above λ is the stage loading that is defined by eq. 2.5.1.1 with the more familiar
notation ψ and μ is the axial speed ratio between station 2 and 3. Station notation can be seen in
figure 17 in section 2.5.2.
In the special case of constant blade speed throughout the stage (v=U2/U3=1) the angles can be
expressed as:
1
𝜙2
𝜆
tan 𝛼2 = 𝜙𝜇 [2 + (1 − 𝑟) − (𝜇2 − 1) 2𝜆 ]
1
𝜆
(2.5.1.8)
𝜙
tan 𝛼3 = 𝜙 [− 2 − (1 − 𝑟) − (𝜇2 − 1) 2𝜆]
1
(2.5.1.9)
𝜙2
𝜆
tan 𝛽2 = 𝜙𝜇 [2 + (1 − 𝑟) − (𝜇2 − 1) 2𝜆 − 1]
1
𝜆
(2.5.1.10)
𝜙
tan 𝛽3 = 𝜙 [− 2 + (1 − 𝑟) − (𝜇2 − 1) 2𝜆 − 1]
(2.5.1.11)
In the further special case where the axial velocity through the stage is constant (μ=Cx2/Cx3=1) making
the flow angles a function of only the three parameters: stage load, stage flow and the reaction.
24
tan 𝛼2 =
1 𝜆
[ +
𝜙 2
1
(1 − 𝑟)]
𝜆
tan 𝛼3 = 𝜙 [− 2 − (1 − 𝑟)]
1 𝜆
tan 𝛽2 = 𝜙 [2 − 𝑟]
1
(2.5.1.12)
(2.5.1.13)
(2.5.1.14)
𝜆
tan 𝛽3 = 𝜙 [− 2 + (1 − 𝑟) − 1]
(2.5.1.15)
As seen later in section 2.5.2 the angles need to be redefined so that zero degree velocity is in the axial
direction. This is simply done as:
The angles from eq. 2.5.1.12-2.5.1.15 then become:
1
𝜆
𝛼2 = tan−1 [𝜙 (2 + (1 − 𝑟))]
1
𝜆
𝛼3 = tan−1 [𝜙 (− 2 − (1 − 𝑟))]
1 𝜆
𝜙 2
𝛽2 = tan−1 [ ( − 𝑟)]
1
𝜙
𝜆
2
𝛽3 = tan−1 [ (− − (1 − 𝑟) − 1)]
(2.5.1.16)
(2.5.1.17)
(2.5.1.18)
(2.5.1.19)
These angle definitions will result in that the angles are positive in nozzle blades direction and
negative in the rotor blades.
Inlet and outlet states of the turbine are known from the results in the ORC program and leave the user
to define five parameters: stage load, reaction, flow coefficient, rotational speed and the mean radius
(assumed constant), i.e. the special case above is used.
Using the flow angles, mean radius, speeds, enthalpy, entropy and pressure as input to the stage
calculation the turbine is built up stage by stage. An initial guess of the number of stages has to be
done and is set to one. This because the program doesn’t work if the guessed number of stages is
higher than actually needed. The number of stages is iterated based on the stage loading defined
earlier. If the required stage load for the last stage is higher than the user defined value another stage is
added. This is repeated until the stage loading of the last stage is less or equal to the defined value.
The last stage is also designed so that the flow angle out of the turbine is small. This is accomplished
by changing the degree of reaction of the last stage. The program tries to set the angle to 10 degrees.
However, if the reaction for that angle is smaller than 0.05 or greater than 0.5 the reaction is set to the
corresponding limit value. Therefore the angle may not necessary be 10 degrees.
The low flow angle is needed as the diffuser, that recovers pressure, otherwise isn’t as effective as it
should be. With this in mind one might think that the outlet flow should be purely axial (0°), however
as there often are supports mounted, the flow is disturbed if the angle are too low and therefore a small
angle is needed.
2.5.1.2 Diffuser
After last stage a diffuser is placed for pressure recovery. Without a diffuser the turbine only can
expand down to the condenser pressure but with a diffuser, a larger expansion in the turbine is made as
25
the static pressure after the last stage can be lowered. Figure 15 shows the expansion with and without
a diffuser and shows that the enthalpy difference is larger with the diffuser than without i.e. the work
output is larger.
Figure 15: Expansion line in the h-s diagram for a turbine with and without a diffuser. P ref is the
condenser static pressure. Station 2 is after the last turbine stage where the 2,D denotes a
diffuser being used and 2 no diffuser.
Mass flow over a diffuser is constant as:
𝑚̇ = 𝑐1 · 𝜌1 · 𝐴1 = 𝑐2 · 𝜌2 · 𝐴2
(2.5.1.20)
Diffuser pressure recovery coefficient is expressed as (general notation as in figure 16):
𝑃 −𝑃
𝐶𝑝 = 𝑃 2 −𝑃1
01
𝐶𝑝 =
(2.5.1.21)
1
𝑃2 −𝑃1
𝑃
𝑃1 ( 01 −1)
(2.5.1.22)
𝑃1
𝑃
𝑃
𝐶𝑝 · ( 𝑃01 − 1) = 𝑃2 − 1
1
1
(2.5.1.23)
26
Figure 16: Diffuser. 1 is after the last rotor (i.e. inlet of diffuser) and 2 is the outlet of the
diffuser. L is the length and B is width of the diffuser.
Using eq. (4.4.1.23) the static pressure after the turbine stage is expressed as:
𝑃1 =
𝑃2
𝑃
1+𝐶𝑝 ·( 01 −1)
(2.5.1.24)
𝑃1
Figure 17: Annular Diffuser-Sovran & Klomp chart. Pressure recovery factor depending on the
area ratio and the length over width ratio. AR= A2/A1. Notation in figure 16
With perfect gas assumed the following relationships can be used:
𝛾
𝑃01
𝑃1
=
𝑇
𝛾−1
( 𝑇01 )
1
𝑇01 = 𝑇1 +
𝑐1 2
2·𝑐𝑝
(2.5.1.25)
(2.5.1.26)
27
𝑐𝑝 = 𝑐𝑣 + 𝑅
𝑐
(2.5.1.27)
𝑅
1 = 𝑐𝑣 + 𝑐
𝑝
𝛾=
(2.5.1.28)
𝑝
𝑐𝑝
(2.5.1.29)
𝑐𝑣
𝛾·𝑅
𝑐𝑝 = 𝛾−1
(2.5.1.30)
Eq. 4.4.1.31 and eq. 4.4.1.27 give:
𝑇01
𝑇1
=1+
𝑐1 2 ·(𝛾−1)
2·𝛾·𝑅·𝑇1
(2.5.1.31)
The Mach number is calculated as:
𝑀𝑎 =
𝑐
(2.5.1.32)
√𝛾𝑅𝑇
Inserting eq. 2.5.1.32 in eq. 2.5.1.31 then gives:
𝑇01
𝑇1
=1+
𝛾−1
2
· 𝑀𝑎1 2
(2.5.1.33)
Using eq. 2.5.1.24, 2.5.1.25 and 2.5.1.33 the pressure before the diffuser is written:
𝑃1 =
𝑃2
𝛾
𝛾1 −1
1+𝐶𝑝 {(1+
𝑀𝑎1 2 )𝛾−1 −1}
2
(2.5.1.34)
P1 is the pressure before the diffuser, i.e. P3 for the last stage, and will be referred to as P3_diffuser so it
not becomes mixed up with the P3 calculated from the stage. Cp is set to a fix value of 0.6. This value
means that the diffuser has quite good pressure recovery and is “medium” sized as seen in figure 17.
The error is calculated as:
𝑒𝑟𝑟𝑜𝑟 = 𝑃3 − 𝑃3𝑑𝑖𝑓𝑓𝑢𝑠𝑒𝑟
(2.5.1.35)
The slope is expressed as [17]:
𝑑𝜓
𝑑𝑃3
≈−
1−𝛾 1
𝛾−1
𝛾
𝛾
∙𝑐𝑝 ∙𝜂𝑠 ∙𝑇01 ∙𝑃01 ∙𝑃03
𝛾
𝑈2
(2.5.1.36)
𝛾
𝑃0
𝑃
= (1 +
𝛾−1
𝛾−1
𝑀𝑎2 )
2
(2.5.1.37)
Eq. 2.5.1.37 shows that the error for higher Mach numbers are small.
Using eq. 2.5.1.2 and Newton-Raphson the new ψ is calculated as:
𝜓𝑛+1 = 𝜓𝑛 − 𝑅𝐿𝑋 ·
𝑒𝑟𝑟𝑜𝑟
𝑑𝜓
𝑑𝑃3
(2.5.1.38)
28
2.5.1.3 Choosing the stage load and reaction
An investigation was carried out by Macchi and Perdichizzi [18] of predicting efficiency of a turbine
stage for nonconventional fluids. They concluded that the optimum stage load and reaction is
dependent on the expansion ratio. This has to do with decreasing the Mach number in the rotor blades.
For high expansion ratios (compressible) the stage load coefficient needs to be smaller than for the
incompressible case with same reaction. The trend is also that higher reaction means the stage load
must decrease. For the large expansion ratios (Vout/Vin = 10) the authors suggest stage load factor of
around 2 down to 1 for the reaction interval of 0.1 to 0.45. The values for the incompressible case,
ranges from around 2.5-2.8 down to 0.7-1 for reactions between 0.08 to 0.68.
2.5.2 Stage calculation
The stage is divided into two iteration loops, stator and rotor loop, both built up in the same way. The
iteration is built on the connection between pressure losses and the increase of entropy.
Figure 18: Schematic of a turbine stage with assumed constant mean radius. N = nozzle and R=
rotor.
Nozzle
Gibbs equation [19] states that:
𝑇0 ∙ 𝑑𝑠 = 𝑑ℎ0 − 𝑣 ∙ 𝑑𝑃0
(2.5.2.1)
Entropy for the total state is the same as for static.
Eq. 2.5.2.1 rewritten gives:
𝑑𝑠 =
𝑑ℎ0
𝑇0
−
𝑣∙𝑑𝑃0
𝑇0
(2.5.2.2)
No work is done across the nozzle, i.e. h02 = h01 and eq. 2.5.2.2 becomes:
𝑑𝑠 = −
𝑣∙𝑑𝑃0
𝑇0
(2.5.2.3)
Assuming perfect gas gives v as:
𝑣=
𝑅∙𝑇0
𝑃0
(2.5.2.4)
Eq. 2.5.2.3 is then temperature independent as:
29
𝑑𝑠 = −
𝑅∙𝑑𝑃0
𝑃0
(2.5.2.5)
By integrating ds, an expression for the entropy difference is found:
𝑠2
𝑃
∫𝑠1 𝑑𝑠 = ∆𝑠 = −𝑅 ∙ ln 𝑃02
01
(2.5.2.6)
The gas constant R is calculated as:
𝑅=
𝑅𝑢
𝑀
(2.5.2.7)
Ru is the universal gas constant and M is the molar weight of the fluid.
All properties of the fluid are found with REFPROP with enthalpy and entropy as in variables. The
loss model AMDCKOMK [20] also used by the gas turbine calculation program LUAX-T is used to
find the losses.
Figure 19: Angle definition for the loss model. Angles are positive in the blades direction i.e.
when the velocity in the direction of the blade the angle is positive.
Angle definition in the loss model is different of that in the flow angle calculation and is seen in
figure 19 where the angles always is positive in blade direction and the zero degree angle means axial
velocity.
Because of the definition in previous section the angles α3 and β3 needs to be called as negative (a
minus sign in front). This is due to that it gives negative angle for the rotor blade direction. The
negative sign when called will make the angle positive, if the velocity is in the blades direction.
30
The annulus are is calculated by using the mass flow, density and axial velocity of the fluid.
𝑚̇
2 ∙𝐶𝑥
𝐴=𝜌
(2.5.2.8)
Blade height is calculated with the annulus area and mean radius as:
2
2
𝐴 = 𝜋 · (𝑟𝑡𝑖𝑝
− 𝑟ℎ𝑢𝑏
)
𝑟𝑚 =
𝑟𝑡𝑖𝑝 +𝑟ℎ𝑢𝑏
(2.5.2.9)
(2.5.2.10)
2
Eq. 2.5.2.9 and 2.5.2.10 give the tip radius:
𝐴
𝑟𝑡𝑖𝑝 = 4·𝜋·𝑟 + 𝑟𝑚
(2.5.2.11)
𝑟ℎ𝑢𝑏 = 2 · 𝑟𝑚 − 𝑟𝑡𝑖𝑝
(2.5.2.12)
𝑚
Reynolds number is expressed as [21]:
𝑅𝑒𝑁 =
𝜌2 ∙𝐶2 ∙𝑐𝑁
𝜇2
(2.5.2.13)
Where density and dynamic viscosity is given by REFPROP and absolute speed from the turbine
program. The blade chord, cN, is calculated with the models lonb1 (returns blade height-axial chord
ratio) and stagger_1 (returns stagger angle, θ). Blade height known from eq. 2.5.2.11- 2.5.2.12 and cN
is easily calculated:
𝑏
𝑐𝑁 = cos 𝜃
(2.5.2.14)
Figure 20: Blade chord c, with axial chord b and stagger angle θ. The pitch is denoted s.
The total loss coefficient, Ytot, returned by AMDCKOMK is expressed in pressure loss as:
𝑌𝑡𝑜𝑡 =
∆𝑃
𝑞
(2.5.2.15)
Where q is the dynamic pressure:
𝑞 = 𝑃02 − 𝑃2 ≈
𝑃­𝛾·𝑀𝑎 2
2
(2.5.2.16)
31
Eq. 2.5.2.5 and 2.5.2.9 then gives the entropy change as a function of loss coefficient and pressure:
∆𝑠 = −𝑅 ∙ ln(1 −
𝑌𝑡𝑜𝑡 ∙(𝑃02 −𝑃2 )
)
𝑃01
(2.5.2.17)
The error is calculated as:
𝑒𝑟𝑟𝑜𝑟 = ∆𝑠𝑛𝑒𝑤 − ∆𝑠𝑜𝑙𝑑
(2.5.2.18)
Rotor
The equations for calculating the nozzle are also valid for the rotor. By using the fact that the relative
work on the rotor is nought, i.e. h03_rel = h02_rel, the equations for the nozzle is also valid for the rotor
because it “acts” as a nozzle relative to the flow. Using the relative values for states 2 and 3 instead of
the absolute the calculation carries out exactly as for the nozzle. To clarify the Reynolds number and
Δs are written as:
𝑅𝑒𝑟𝑜𝑡 =
𝜌3 ∙𝑊3 ∙𝑐𝑟
𝜇3
∆𝑠 = −𝑅 ∙ ln(1 −
(2.5.2.19)
𝑌𝑡𝑜𝑡 ∙(𝑃03_𝑟𝑒𝑙 −𝑃3 )
𝑃02_𝑟𝑒𝑙
)
(2.5.2.20)
32
Mach
Pressure
Entropy
Enthalpy
Turbine calc
Flow angles,
absolute
components
Flow angles,
relative
components
Mach
Pressure
Entropy
Enthalpy
guess ”old ds”
error > 0.1
guess ”old ds”
ds=
old ds + error
ds=
old ds + error
ZweStaSBC1,
lonb1,
Ang_stagger
ZweStaSBC1,
lonb1,
Ang_stagger
Input values
AMDCKOMK
Input values
AMDCKOMK
AMDCKOMK
AMDCKOMK
Loss koeff.
Y_tot
Loss koeff.
Y_tot
New ds
error=
new ds - old ds
New ds
error < 0.1
error=
new ds - old ds
error > 0.1
error < 0.1
Turbine calc
Figure 21: Flow chart of the stage calculation. Left loop is the stator and the right the rotor.
33
34
3 Result
This section presents the result from the modified program running the two fluids pentane and R134a.
Sections 5.1.1-5.1.4 shows the different cycles and mass flow. Section 5.1.5 shows an example of the
main program that’s done a subcritical calculation.
3.1 Result from the main code
Assumptions made: Turbine and pump efficiency’s set to 85 % and 80 % respectively. Initial reheater
efficiency set to 80 %. No pressure drops in the heat exchangers. Pinch between highest cycle
temperature and heating media is set to 10 °C. Thermal oil as heat source with a mass flow set to
1 kg/s. Pressure range is set from 2 to 25 bar with steps of 0.1 bar. No mechanical losses are
considered. The result section only consider subcritical cycles.
The x axis is the heat source temperature and the number at the end of each line is the temperature of
the coolant.
3.1.1 Saturated
The maxmimum temperature of the fluid is the saturation temperatures. Instead of raising the
temperature closer to the heating media the mass flow is increased.
Figure 22: Cycle efficency of the saturated cycle
35
Figure 23: Power output curves of the saturated cycle.
Figure 24: Total efficiency of the saturated cycle
The power curves sudden change seen for pentane around 240 °C has to do with the pinch-point in the
preheater have been adjusted so that the mass boiled isn’t greater than what can be preheated. This also
explains why the total efficiency has a sudden change, as more and more of the heat available is not
being used when the pinch point increase. The same goes for R134a but for a lower heating
temperature. This explains why the total efficiency levels out while the power is increasing.
36
3.1.2 Superheated with no evaporation in reheater
Cycle temperature set to the oil temperatures minus the pinch.
Figure 25: Cycle efficiency of the superheated cycle with no evaporation in the reheater.
Figure 26: Power curves of the superheated cycle with no evaporation in the reheater.
37
Figure 27: Total efficiency of the superheated cycle with no evaporation in the reheater.
The decrease in cycle efficiency for pentane is explained by the reheater. The preheater was set to
always exist and therefore, for the higher temperatures, the reheater efficiency was decreased until
state 3 lies beneath state 7 in the T-s diagram. The total efficiency on the other hand increases as more
of the heat source is used. R134a has a break point for the superheated cycles as the fluids temperature
is following the heat source instead of saturation temperature. This means that R134a:s TPFLSH
temperature is reached and therefore can’t go further.
3.1.3 Superheating with evaporation allowed in reheater
In this case the fluid is allowed to evaporate between state 2 and 3 if the transferable heat is enough. If
it’s enough to evaporate then the preheater is removed and the evaporator comes after the reheater.
Figure 28: Cycle efficiency with evaporation allowed in the reheater i.e. when this occurs the
preheater is removed
38
Figure 29: Power curves with evaporation allowed in the reheater
Figure 30: Total efficiency with evaporation allowed in the reheater
Boiling in the preheater is allowed and when it occurs the preheater is removed. This doesn’t affect the
power and total efficiency much however the cycle efficiency becomes the highest of the three cases.
39
3.1.4 Mass flow superheated and saturated
Following graph shows the mass flow of the saturated cycle and the superheated with no evaporation
in the reheater.
Figure 31: Mass flows of the saturated and superheated cycles from the power curves with 10 ºC
cooling. Solid line for the saturated and dashed for the superheated.
As seen the mass flow is greater for the saturated cycle, especially as the temperature goes up. The
saturated cycle of R134a can also be used for a longer temperature range than the superheated as the
fluid temperature never goes above the saturation temperature.
40
3.2 The Main Program
Figure 31 shows a calculation made by the program for all the fluids. The heat source were set at
160 °C with a mass flow of 10 kg/s. Pressure range were set 5 to 25 bar with 10 °C superheating. The
result was that R227ea gave the highest power output for this case.
Figure 32: Example of the program for a subcritical calculation. Input values on the left side of
the program and result section on the right. Note that the program finished although it says
working. This box is supposed to turn green but there’s a bug.
41
4 Discussion
The figures show the efficiency and power curves of two mediums for three different cases. As seen in
figure 23 the highest power output comes from the saturated cycle while the highest cycle efficiency
comes from when the media is allowed to evaporate in the reheater thus removing the preheater. The
total efficiency gives the same result as the power curves. This means that the preferred cycle is the
saturated as it gives the highest power output and the highest total efficiency. Note that because values
in the figures are the maximums of a range of pressures the highest cycle efficiency may be on a
different pressure than the maximum power in respective cycle. Also optimal pressure can differ for
the same fluid on different cooling temperatures.
Though only two mediums are shown for three different cases in result, the problem with finding an
optimum fluid can be seen. A closer look on one of the superheated results shows that R134a higher
power output than pentane up to its break point and for the coldest cooling temperature. When the
cooling temperature goes up the performance of R134a comes closer to pentane and eventually
perform worse over a certain cooling and heating temperature. The heat source temperature where the
lines cross decreases as the cooling temperature goes up. The same trend is seen on the saturated
although it has no breakpoints as the temperature of the fluid never exceeds saturation temperature.
A fluid with a low critical temperature often has high critical pressure. This means that also the
condensation pressure is higher than for a fluid with lower critical pressure. Therefore, for a fix
maximum pressure, the performance is greatly affected by the condenser pressure i.e. the condenser
temperature. With a higher condensation temperature a low critical pressure fluid performance will be
better at lower heating temperatures compared to a high critical pressure fluid.
However R134acan produce electrical power with heating temperatures as low as 60 °C, although not
much, while pentane needs a temperature almost 20 °C higher than that. As said the power production
is very small, <5 kW for this temperature on 1 kg/s of the heat source. This do not seems as much but
if the heat source used is the return line from district heating there are big mass flows involved thus
resulting in quite high power output for the very low grade heat source, not taking into account the
size of the components as a result of the high mass flow.
The increased power output from saturated cycle is explained by figure 31. As seen the mass flow
increases with the temperature more rapid than the superheated which leads to higher power output.
Because there’s no superheating the mass flow can be increased more than for the superheated cycles
thus for maximum power output the saturated cycle is preferred. Problems may arise with saturated
cycle as moisture can form and damage the turbine. For dry and isentropic fluids, problems with
moisture occur at inlet of the turbine as the outlet is superheated while for wet fluids it can occur both
at inlet and outlet. The cycle efficiency becomes constant as the specific work, both out and in, and the
specific heat in become constant.
The small decrease of the mass flow for saturated pentane is hard to explain. The curve as a whole
follows the expected trend that it increases with the temperature. One explanation could be that the
power of this point where found for two different pressure levels and therefore the “wrong” mass flow
was picked. Another explanation could be that REFPROP calculated the states erroneously for this
point thus giving a high power output for lower mass flow.
The cycle that allows boiling in the reheater has best cycle efficiency of the three while its power
output is similar to that of the superheated. However, with ORC cycle using waste heat, the highest
cycle efficiency is not as interesting as the highest power because the heat source from the beginning
42
is a loss. Cycle efficiency, as can be seen in all the cycles, can also be misleading. Efficiency can be
quite high but the power output small, i.e. most of the heat available isn’t used. Therefore the more
correct comparison is to look at the power output or the total efficiency which gives a better
comparison between mediums. When there’s a fix heat source the comparison between fluids should
be done by either the power output or the total efficiency while the cycle efficiency is useful when the
heat source can be adjusted.
As stated earlier superheating has a negative influence on the total efficiency and power output and for
dry fluids it should be avoided. The wet fluids can however sometimes benefit from superheating [22]
and it’s safer for the turbine as less moisture occur when superheated compared to saturated. With this
result it’s shown that best way for the ORC program is to let the user decide how many degrees of
superheating to have instead of setting the pinch between the heating medium and working fluid. A
small amount of superheating can be preferable even for dry fluids to ensure that there’s no moisture at
the inlet of the turbine.
The main program, seen in section 5.1.5 gives the user the cycle performance numbers with the T-s
and T-Q diagrams. The result section gives the user information on what fluid performed best, in what
cycle and the performance data such as efficiency, power output and mass flow.
The results show the thermo dynamical performance of the optimum fluid for the particular case. By
pressing the button Turbine calculation the optional turbine calculation can be made. The needed
properties (e.g. pressure, enthalpy, entropy) before and after the turbine are imported for the resulting
fluid. With the imported values and defining the five design parameters the turbine is calculated. Note
that the ORC program must have made a calculation and the window is still open for the turbine
program to work.
The number of fluids that could be run is quite few considering how many fluids there is. However as
the 12 chosen are from other reports under different conditions they should suffice. A problem could
occur thou, especially for the refrigerants as legislations can make them illegal to use as they often
have high global warming potential. In the future an exchange of some of the fluids might be
necessary. More fluids could potentially be added by adding more pages of fluids if needed.
43
44
5 Conclusion and Future Work
5.1 Conclusion







The subcritical cycle should as close to saturated as possible.
The dry fluids only should be running almost on the saturation curve while the wet should
only superheat until an acceptable level of moisture in the end of expansion is achieved.
The cooling temperature has a large impact on the performance. Changing the cooling
temperature can change what the optimal fluid is for a fix heating temperature
As the result is made over a pressure range the program is useful as it finds the specific values
for the optimum fluid for a certain case.
The cycle and total efficiency’s temperature breakpoints or maximums differ except for the
cycle that allows evaporation in the reheater. The cycle efficiency reaches its maximum at a
lower temperature than the total and for the evaporation in the reheater they are the same.
The cycle efficiency is a good measurement in theory when the heat source can be adjusted as
it is a measure of how well the fluid performs. In practice however it’s not useful as the
maximum power output can’t be related to the cycle efficiency. The cycle does not consider
how much of the energy available is used as only the temperature of the heat source sets it
limits and is independent of mass flows.
For real cycle comparing the power output or the total efficiency is a better measurement of
performance of a fluid as these gives the real maximum values of the fluid. For a specific case
these values is the best when comparing multiple fluids.
5.2 Future work
5.2.1 ORC program
The ORC program has only twelve fluids can be chosen giving the user limited option on fluid
selection. The list of fluids could be increased. Caution with adding more fluids has to be made though
as REFPROP labeling of the fluids isn’t always logical.
The heat source would benefit from a greater selection. E.g. the ability to handle flue gases. Now the
flue gases have to be heat exchanged to water or oil.
The overcritical calculations, especially when using water is quite slow and therefore leaves room for
improvement.
5.2.2 Turbine
The turbine program has difficulty calculating supercritical cycles and for fluids ending their
expansion in the moist region. This needs improving so that the program can handle them.
45
46
6 Program use
This section gives a small guide of how to use the program by doing a calculation. Each of the stations
is briefly explained and lastly a run trough of the buttons is done. Blue rectangles are used to show
what section that have been changed from the figure before.
6.1.1 Initial screen showing on startup.
This screen shows when the program is started.
Figure 33: Initial screen when started
The user starts with selecting the heat source, oil or water. Continued the mass flow and temperature is
set and in the case of water also the pressure needs to be selected.
6.1.2 Heat source selected
The heat source was selected to be oil and with a temperature of 150 ºC and a mass flow of 10 kg/s.
Because no pressure needs to be set for this heat source this field is left blank.
47
Figure 34: The heat source defined.
The cycle properties now need to be set. The starting pressure and pressure is selected. If only one
pressure is to be tested the start and end pressure are set to the same value and step is set to any value
greater than nought. If a range of pressures is to be tested (end pressure > start pressure) the field step
is set with what interval the pressures are going to be tested.
The field overheat sets how many degrees of superheating the cycle is to have. If only a saturated
cycle is desired (no superheating) this field is set to nought.
6.1.3 Cycle properties selected
The pressure were set to start at 2 bar and run with 1 bar interval up to 25 bar. The superheating were
set to 5 ºC (i.e. the state 4 temperature is 5 ºC higher than saturation temperature).
48
Figure 35: The cycle properties chosen.
The next step is to set the efficiency of the pump and turbine.
6.1.4 Component Data
The isentropic efficiency of the turbine was set to 85 % and the pump was set to 80 %.
Figure 36: Pump and Turbine efficiencies chosen
49
Now the fluids need to be set. There are twelve to choose from. User can select one or more for the
calculation. If all fluids are to be tested the button “select all” (circled in figure 36) can be pressed
rather than clicking on every fluid.
6.1.5 Substances
In this case all the fluids were selected to run by pressing “select all”.
Figure 37: Fluids chosen
The properties of the cooling media now need to be selected. The choice is between using water or air
for cooling. After clicking on what media to use a box appear where the temperature the cooling media
is to be set. If the default values in the program want to be used (10 ºC for water and 25 ºC for air) the
box “default temp in” can be clicked and the values are loaded.
Also the ambient temperature needs to be set. If air was selected the ambient temperature is to be set to
the same value as for cooling temperature while for water the temperatures doesn’t need to be the
same.
6.1.6 Cooling
Water was selected with its default value of 10 ºC. The ambient temperature was set to 20 ºC.
50
Figure 38: Cooling selected
Now the values for the heat exchangers need to be set. There are five parameters to set which are:
1.
2.
3.
4.
5.
Efficiency reheater (80 %)
Pinch-point condenser (2 ºC)
Temperature rise of the coolant (10 ºC)
Pressure drop in the heat exchangers (5 %)
Pinch-point of the preheater (10 ºC)
The numbers in the brackets are the predefined numbers that will be loaded by pressing “Use default
values” (encircled in figure 38).
6.1.7 End result
The heat exchangers are using the default values. By deciding what to search for, highest power output
or highest cycle efficiency and then pressing “calculate” the program starts to calculate for all the
fluids selected. The end result is seen in figure 39 where the highest power was decided to be searched
for.
51
Figure 39: Heat exchangers and what to search for chosen. The end result displayed.
The result shows the data of the cycle that delivered the highest power output. Besides what fluid,
power output and efficiencies the temperature of the heat source and cooling outlet is shown. In this
particular case the best fluid needed to move its preheater pinch point and therefore also this is
displayed. Below the results the T-s and T-Q diagrams have been plotted. Figure 40 is also displayed
showing the temperatures and pressures in all the points of the cycle.
If for some reason the user wants to save or enlarge the diagrams this can easily be done. Right click in
the graph and choose “open plot in new window”. The diagram then is opened in a fig file from where
it can be saved.
52
Figure 40: The tempeartures and pressures of the points in the cycle displayed
A few of buttons in program have not been mentioned yet but are presented here with what they do.
1. “clear result”: clears the “Result & Plots” section still leaving the indata. Useful if a single indata
value is to be changed.
2. “reset”: Clears both the indata section and results section.
3. “deselect all”: Is the inverse to the button “select all”. Deselects all of the fluids.
4. “Turbine Calculation”: Opens the turbine calculation program and imports the values needed from
the ORC program to compute the turbine.
53
54
7 References
[1] Energimyndigheten, “Energiläget 2011,” Energimyndigheten, Eskilstuna, 2011.
[2] S. Quoilin, S. Declaye, B. F. Tchanche and V. Lemort, “Thermo-economic optimization of waste
heat recovery Organic Rankine Cycles,” Applied Thermal Engineering, no. 31, 2011.
[3] B. Saleh, G. Koglbauer, M. Wendland and J. Fischer, “Working fluids for low-temperature
organic Rankine cycles,” Energy, vol. 32, no. 7, 2007.
[4] L. K. Nash, “Trouton and T-H-E Rule,” Journal of Chemical Education, vol. 61, no. 11, 1984.
[5] E. Lemmon, M. Huber and M. McLinden, NIST Standard Reference Database 23: Reference
Fluid Thermodynamic and Transport Properties-REFPROP, Version 9.0, Gaithersburg: National
Institute of Standards and Technology, Standard Reference Data Program, 2010.
[6] C. He, C. Liu, H. Gao, H. Xie, Y. Li, S. Wu and J. Xu, “The optimal evaporation temperature and
working fluids for subcritical organic Rankine cycle,” Energy, no. 38, 2012.
[7] J. Roy, M. Mishra and A. Misra, “Performance analysis of an Organic Rankine Cycle with
superheating under different heat source temperature conditions,” Applied Energy, no. 88, 2011.
[8] H. M. Hettiarachchi, M. Golubovic, W. M. Worek and Y. Ikegami, “Optimum design criteria for
an Organic Rankine cycle using low-temperature geothermal heat sources,” Energy, no. 32, 2007.
[9] P. J. Mago, L. M. Chamra, K. Srinivasan and C. Somayaji, “An examination of regenerative
organic Rankine cycles using dry fluids,” Applied Thermal Engineering, no. 28, 2008.
[10] A. A. Lakew and O. Bolland, “Working fluids for low-temperature heat source,” Applied Thermal
Engineering, no. 30, 2010.
[11] N. A. Lai, M. Wendland and J. Fischer, “Working fluids for high-temperature organic Rankine
cycles,” Energy, no. 36, 2011.
[12] B. F. Tchanche, G. Papadakis, G. Lambrinos and A. Frangoudakis, “Fluid selection for a lowtemperature solar organic Rankine cycle,” Apllied Thermal Engineering, no. 29, 2009.
[13] B. Sundén, “Värmeöverföring,” Lund, 2006, p. 333.
[14] D. W. GREEN and R. H. PERRY, “PERRY'S CHEMICAL ENGINEERS' HANDBOOK 8th
edition,” pp. 2-185.
[15] S. L. Dixon and C. A. Hall, Fluid Mechanics and Thermodynamics of Turbomachinery, 6 ed.,
2010.
[16] M. Schobeiri, Turbomachinery Flow Physics and Dynamic Performance, 2005.
55
[17] D. Olsson, “LUAX-T,” Lund, 2008.
[18] E. Macchi and A. Perdichizzi, “Efficiency Prediction for Axial-Flow Turbines Operating with
Nonconventional Fluids,” Journal of engineering for power, pp. 718-724, 1981.
[19] Y. A. Cengel and M. A. Boles, THERMODYNAMICS An Engineering Approach, 6th ed., 2007.
[20] H. Moustapha, M. F. Zelesky, N. C. Baines and D. Japikse, Axial and Radial Turbines, Vermont:
Concepts ETI, 2003.
[21] H. Saravanamuttoo, G. Rogers, h. Cohen and P. Straznicky, Gas turbine Theory, 6th ed. ed., 2009.
[22] H. Chen, D. Y. Goswami and E. K. Stefanakos, “A review of thermodynamic cycles and working
fluids for the conversion of low-grade heat,” Renewable and Sustainable Energy Reviews, no. 14,
2010.
56
8 Appendix A
8.1 ORC Program
function varargout = ORC(varargin)
%#####################################################################
%##
##
%##
##
%##
Mikael Olsson 2012
##
%##
##
%##
##
%#####################################################################
%
%HEAT SOURCE
%Choose whether you have thermal oil (oil) or water. Oil uses the
%oil_source.m and h_diff.m files for iteration & entalphy difference. No
%pressure needs to be defined. Water uses the water_source.m file for
%iteration only.
%A pressure needs to be defined for water, thats in the subcooled area for
%the given temperature.
%
%CYCLE PROPERTIES
%Set your starting pressure,range and end pressure thats is going to be
%calculated. If only one pressure is to be calculated set the start and end
%pressure to the same value and steps to any number >0.
%The overheat input is how many degrees it should superheat. If no
%superheating is wanted set this value to 0. Then no superheater is needed.
%
%COMPONENT DATA
%Enter the isentropic efficencys of turbine and pump. The value is to be in
%percent, NOT decimals. E.g for 85% efficeny, enter 85, not 0.85;
%
%SUBSTANCE
%Select which substance/substances to try.
%
%COOLING
%Select if water or air is used as condensor cooling. Enter what
temperature
%the cooling media has at condensor inlet or click the box "Default Temp
%In" to use default temperatures. For water it is 10 C and air 25 C.
%
%PINCH-POINTS & REHEATER EFFICENY
%Efficency Reheater: If no reheater is to be used, set this value to 0 else
%the value is to be in percent, NOT decimals. E.g 80%, not 0.8. Default
%value for this is set to 80%
%
%Pinch-Point condenser: Temperature difference between cooling medie and
%working fluid at starting point of condensation. Default value set to 2 C.
%
%Temperature rise coolant: Temperature difference of the cooling medie at
%inlet and start of condensation. Default value set to 10 C.
%
%Pressuredrop Hex: Pressure drop in the heat exchangers on the working
%fluid side. Default value set to 5%.
%
%Pinch-Point Preheater: Temperature difference between the sat. liquid and
%the heat source after the preheater. Default value set to 10 C.
%
%SEARCH FOR
57
%Choose what you want to find, highest power or efficency.
%
%PUSHBUTTONS
%Calculate starts the calculation
%Reset clears "Indata","Search for" & "Result&Plots".
%clear result only clears the "Result&Plots".
%
%IMPORTANT!!!
%If the numbers and letters in the plots are upside down after
%calculating or opening in seperate figure it might be a problem with the
%hardware of the machine and matlab (at least for ver.2009b). To get around
%this, type "opengl info" in command window. If "Software = false"
%type: "opengl software". Then type "opengl info" again and it should
%say: "software=true". Now the numbers and letters always should be the
%right way up when program is restarted or "clear result" has been pushed.
%This has to be done every time matlab has been closed.
%
%Caution!!!
%When doing supercritical cycles (typically P>30-35 bar) and using
%water as heat source the iteration is slow because the communication
%between matlab and refprop. Therefore its recomended to only do one
%fluid at a time when running supercritical cycles with water as heat
%source.
%
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%
LLL
TTTTTTTTTTTTTT
HHH
HHH
%
LLL
TTTTTTTTTTTTTT
HHH
HHH
%
LLL
TTT
HHH
HHH
%
LLL
TTT
HHH
HHH
%
LLL
TTT
HHHHHHHHHHHHHH
%
LLL
TTT
HHHHHHHHHHHHHH
%
LLL
TTT
HHH
HHH
%
LLL
TTT
HHH
HHH
%
LLLLLLLLLLLL TTT
HHH
HHH
%
LLLLLLLLLLLL TTT
HHH
HHH
%
% See also: GUIDE, GUIDATA, GUIHANDLES
% Edit the above text to modify the response to help ORC
% Last Modified by GUIDE v2.5 26-Jun-2012 09:24:21
% Begin initialization code - DO NOT EDIT
gui_Singleton = 1;
gui_State = struct('gui_Name',
mfilename, ...
'gui_Singleton', gui_Singleton, ...
'gui_OpeningFcn', @ORC_OpeningFcn, ...
'gui_OutputFcn', @ORC_OutputFcn, ...
'gui_LayoutFcn', [] , ...
'gui_Callback',
[]);
if nargin && ischar(varargin{1})
gui_State.gui_Callback = str2func(varargin{1});
end
if nargout
[varargout{1:nargout}] = gui_mainfcn(gui_State, varargin{:});
else
gui_mainfcn(gui_State, varargin{:});
end
% End initialization code - DO NOT EDIT
clc;
58
% --- Executes just before ORC is made visible.
function ORC_OpeningFcn(hObject, eventdata, handles, varargin)
% This function has no output args, see OutputFcn.
% hObject
handle to figure
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% varargin
command line arguments to ORC (see VARARGIN)
% Choose default command line output for ORC
handles.output = hObject;
%Add logo
bild2 = imread('Logo.bmp');
axes(handles.logo);
imshow(bild2);
set(handles.logo,'HandleVisibility','off')
axis off
set(handles.pp_new_descrip,'Visible','off');
set(handles.pp_new,'Visible','off');
set(handles.pp_new_unit,'Visible','off');
set(handles.text88,'Visible','off');
set(handles.temp_coolt,'Visible','off');
set(handles.Turb_calc,'Visible','off');
guidata(hObject, handles);
% UIWAIT makes ORC wait for user response (see UIRESUME)
% uiwait(handles.figure1);
% --- Outputs from this function are returned to the command line.
function varargout = ORC_OutputFcn(hObject, eventdata, handles)
% varargout cell array for returning output args (see VARARGOUT);
% hObject
handle to figure
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Get default command line output from handles structure
varargout{1} = handles.output;
function effic_t_Callback(hObject, eventdata, handles)
% hObject
handle to effic_t (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of effic_t as text
%
str2double(get(hObject,'String')) returns contents of effic_t as a
double
effic_t =str2double(get(hObject,'String'));
if isnan(effic_t)
set(hObject, 'String', 0);
errordlg('Input must be a number','Error','on');
end
handles.val.effic_t = effic_t;
guidata(hObject,handles)
59
% --- Executes during object creation, after setting all properties.
function effic_t_CreateFcn(hObject, eventdata, handles)
% hObject
handle to effic_t (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
function effic_p_Callback(hObject, eventdata, handles)
% hObject
handle to effic_p (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of effic_p as text
%
str2double(get(hObject,'String')) returns contents of effic_p as a
double
effic_p =str2double(get(hObject,'String'));
if isnan(effic_p)
set(hObject, 'String', 0);
errordlg('Input must be a number','Error','on');
end
handles.val.effic_p = effic_p;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function effic_p_CreateFcn(hObject, eventdata, handles)
% hObject
handle to effic_p (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
function start_pressure_Callback(hObject, eventdata, handles)
% hObject
handle to start_pressure (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of start_pressure as text
%
str2double(get(hObject,'String')) returns contents of
start_pressure as a double
start_pressure =str2double(get(hObject,'String'));
if isnan(start_pressure)
set(hObject, 'String', 0);
errordlg('Input must be a number','Error','on');
60
end
handles.val.start_pressure = start_pressure;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function start_pressure_CreateFcn(hObject, eventdata, handles)
% hObject
handle to start_pressure (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
function steps_Callback(hObject, eventdata, handles)
% hObject
handle to steps (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of steps as text
%
str2double(get(hObject,'String')) returns contents of steps as a
double
steps =str2double(get(hObject,'String'));
if isnan(steps)
set(hObject, 'String', 0);
errordlg('Input must be a number','Error','on');
end
handles.val.steps = steps;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function steps_CreateFcn(hObject, eventdata, handles)
% hObject
handle to steps (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
function end_pressure_Callback(hObject, eventdata, handles)
% hObject
handle to end_pressure (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of end_pressure as text
%
str2double(get(hObject,'String')) returns contents of end_pressure
as a double
end_pressure =str2double(get(hObject,'String'));
if isnan(end_pressure)
set(hObject, 'String', 0);
errordlg('Input must be a number','Error','on');
end
61
handles.val.end_pressure = end_pressure;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function end_pressure_CreateFcn(hObject, eventdata, handles)
% hObject
handle to end_pressure (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
function overheat_Callback(hObject, eventdata, handles)
% hObject
handle to overheat (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of overheat as text
%
str2double(get(hObject,'String')) returns contents of overheat as
a double
overheat =str2double(get(hObject,'String'));
if isnan(overheat)
set(hObject, 'String', 0);
errordlg('Input must be a number','Error','on');
end
handles.val.overheat = overheat;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function overheat_CreateFcn(hObject, eventdata, handles)
% hObject
handle to overheat (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
% --- Executes on button press in oil_heat.
function oil_heat_Callback(hObject, eventdata, handles)
% hObject
handle to oil_heat (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
if (get(hObject,'Value')==get(hObject,'Max'))
minVal = get(handles.water_heat,'Min');
set(handles.water_heat,'Value',minVal);
end
% if (get(hObject,'Value')==get(hObject,'Min'))
%
maxVal = get(handles.water_heat,'Max');
%
set(handles.water_heat,'Value',maxVal);
% end
62
set(handles.mass_heat,'String','Massflow oil')
set(handles.temp_heat,'String','Oil temperature in')
set(handles.pressure_heat,'String','Not in use for oil')
%set(handles.pressure_in,'String','Only used if heat source is water')
% set(handles.pressure_in,'Visible','off')
% set(handles.text48,'Visible','off')
% Hint: get(hObject,'Value') returns toggle state of oil_heat
% --- Executes on button press in water_heat.
function water_heat_Callback(hObject, eventdata, handles)
% hObject
handle to water_heat (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
if (get(hObject,'Value')==get(hObject,'Max'))
minVal = get(handles.oil_heat,'Min');
set(handles.oil_heat,'Value',minVal);
end
% if (get(hObject,'Value')==get(hObject,'Min'))
%
maxVal = get(handles.oil_heat,'Max');
%
set(handles.oil_heat,'Value',maxVal);
% end
set(handles.mass_heat,'String','Massflow water')
set(handles.temp_heat,'String','Water temperature in')
set(handles.pressure_heat,'String','Water pressure')
%set(handles.pressure_in,'String','0')
% set(handles.pressure_heat,'Visible','on')
% set(handles.pressure_in,'Visible','on')
set(handles.text48,'String','Bar')
% set(handles.text48,'Visible','on')
% Hint: get(hObject,'Value') returns toggle state of water_heat
function massflow_Callback(hObject, eventdata, handles)
% hObject
handle to massflow (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of massflow as text
%
str2double(get(hObject,'String')) returns contents of massflow as
a double
massflow =str2double(get(hObject,'String'));
if isnan(massflow)
set(hObject, 'String', 0);
errordlg('Input must be a number','Error','on');
end
handles.val.massflow = massflow;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function massflow_CreateFcn(hObject, eventdata, handles)
% hObject
handle to massflow (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
63
end
function temperature_heat_Callback(hObject, eventdata, handles)
% hObject
handle to temperature_heat (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of temperature_heat as text
%
str2double(get(hObject,'String')) returns contents of
temperature_heat as a double
temperature_heat =str2double(get(hObject,'String'));
if isnan(temperature_heat)
set(hObject, 'String', 0);
errordlg('Input must be a number','Error','on');
end
handles.val.temperature_heat = temperature_heat;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function temperature_heat_CreateFcn(hObject, eventdata, handles)
% hObject
handle to temperature_heat (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
function pressure_in_Callback(hObject, eventdata, handles)
% hObject
handle to pressure_in (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of pressure_in as text
%
str2double(get(hObject,'String')) returns contents of pressure_in
as a double
pressure_in =str2double(get(hObject,'String'));
if isnan(pressure_in)&&
(get(handles.water_heat,'Value')==get(handles.water_heat,'Max'))
set(hObject, 'String', 0);
errordlg('Input must be a number','Error','on');
end
handles.val.pressure_in = pressure_in;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function pressure_in_CreateFcn(hObject, eventdata, handles)
% hObject
handle to pressure_in (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
64
end
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%Lägg in alla ämnen här under.
% --- Executes on button press in pentane.
function pentane_Callback(hObject, eventdata, handles)
% hObject
handle to pentane (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hint: get(hObject,'Value') returns toggle state of pentane
% if (get(hObject,'Value') == get(hObject,'Max'))
%
set(hObject,'Value',1);
% end
% --- Executes on button press in butane.
function butane_Callback(hObject, eventdata, handles)
% hObject
handle to butane (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hint: get(hObject,'Value') returns toggle state of butane
% --- Executes on button press in R227ea.
function R227ea_Callback(hObject, eventdata, handles)
% hObject
handle to R227ea (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hint: get(hObject,'Value') returns toggle state of R227ea
% --- Executes on button press in ammonia.
function ammonia_Callback(hObject, eventdata, handles)
% hObject
handle to ammonia (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hint: get(hObject,'Value') returns toggle state of ammonia
% --- Executes on button press in R134a.
function R134a_Callback(hObject, eventdata, handles)
% hObject
handle to R134a (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hint: get(hObject,'Value') returns toggle state of R134a
% --- Executes on button press in R114.
function R114_Callback(hObject, eventdata, handles)
% hObject
handle to R114 (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hint: get(hObject,'Value') returns toggle state of R114
% --- Executes on button press in R245fa.
function R245fa_Callback(hObject, eventdata, handles)
% hObject
handle to R245fa (see GCBO)
65
% eventdata
% handles
reserved - to be defined in a future version of MATLAB
structure with handles and user data (see GUIDATA)
% Hint: get(hObject,'Value') returns toggle state of R245fa
% --- Executes on button press in R113.
function R113_Callback(hObject, eventdata, handles)
% hObject
handle to R113 (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hint: get(hObject,'Value') returns toggle state of R113
% --- Executes on button press in R123.
function R123_Callback(hObject, eventdata, handles)
% hObject
handle to R123 (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hint: get(hObject,'Value') returns toggle state of R123
% --- Executes on button press in R141b.
function R141b_Callback(hObject, eventdata, handles)
% hObject
handle to R141b (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hint: get(hObject,'Value') returns toggle state of R141b
% --- Executes on button press in isopentane.
function isopentane_Callback(hObject, eventdata, handles)
% hObject
handle to isopentane (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hint: get(hObject,'Value') returns toggle state of isopentane
% --- Executes on button press in cyc_pentane.
function cyc_pentane_Callback(hObject, eventdata, handles)
% hObject
handle to cyc_pentane (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hint: get(hObject,'Value') returns toggle state of cyc_pentane
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%%%%%%%%%Kylning%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
% --- Executes on button press in water_cool.
function water_cool_Callback(hObject, eventdata, handles)
% hObject
handle to water_cool (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
66
set(handles.text88,'Visible','on');
set(handles.temp_coolt,'Visible','on');
set(handles.temp_coolt,'style','edit')
set(handles.temp_coolt,'String','0')
set(handles.temp_coolt,'BackgroundColor','white')
set(handles.default_temp_in,'Value',0)
if (get(hObject,'Value')==get(hObject,'Max'))
minVal = get(handles.air_cool,'Min');
set(handles.air_cool,'Value',minVal);
set(handles.temp_coolt,'style','edit')
end
% Hint: get(hObject,'Value') returns toggle state of water_cool
% --- Executes on button press in air_cool.
function air_cool_Callback(hObject, eventdata, handles)
% hObject
handle to air_cool (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
set(handles.text88,'Visible','on');
set(handles.temp_coolt,'Visible','on');
set(handles.temp_coolt,'style','edit')
set(handles.temp_coolt,'String','0')
set(handles.temp_coolt,'BackgroundColor','white')
set(handles.default_temp_in,'Value',0)
if (get(hObject,'Value')==get(hObject,'Max'))
minVal = get(handles.water_cool,'Min');
set(handles.water_cool,'Value',minVal);
end
% Hint: get(hObject,'Value') returns toggle state of air_cool
function ambient_Callback(hObject, eventdata, handles)
% hObject
handle to ambient (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
ambient =str2double(get(hObject,'String'));
if isnan(ambient)
set(hObject, 'String', 0);
errordlg('Input must be a number','Error','on');
end
handles.val.ambient = ambient;
guidata(hObject,handles)
% Hints: get(hObject,'String') returns contents of ambient as text
%
str2double(get(hObject,'String')) returns contents of ambient as a
double
% --- Executes during object creation, after setting all properties.
function ambient_CreateFcn(hObject, eventdata, handles)
% hObject
handle to ambient (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
67
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%% Calculation & PLOT %%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
% --- Executes on button press in calculate.
function calculate_Callback(hObject, eventdata, handles)
% hObject
% eventdata
% handles
handle to calculate (see GCBO)
reserved - to be defined in a future version of MATLAB
structure with handles and user data (see GUIDATA)
set(handles.pp_new_descrip,'Visible','off');
set(handles.pp_new,'Visible','off');
set(handles.pp_new_unit,'Visible','off');
cla(handles.wait)
set(handles.wait,'BackgroundColor','red')
set(handles.wait,'String','Working')
set(handles.uipanel13,'BackgroundColor',[0.94,0.94,0.94])
set(handles.uipanel18,'BackgroundColor',[0.94,0.94,0.94])
if
(get(handles.water_heat,'Value')==get(handles.water_heat,'Min'))&&(get(hand
les.oil_heat,'Value')==get(handles.oil_heat,'Min'))
errordlg('Choose heatsource medie','Error','on')
return;
end
if
(get(handles.water_cool,'Value')==get(handles.water_cool,'Min'))&&(get(hand
les.air_cool,'Value')==get(handles.air_cool,'Min'))
errordlg('Choose coolant','Error','on')
set(handles.uipanel18,'BackgroundColor','red')
set(handles.wait,'BackgroundColor','red');
set(handles.wait,'String','Error');
end
cla(handles.T_s);
cla(handles.T_Q);
if (get(handles.water_heat,'Value')==get(handles.water_heat,'Max'))
if handles.val.pressure_in<1
errordlg('You must set a pressure for the water','Error','on')
return;
end
if
refpropm('Q','T',handles.val.temperature_heat+273.15,'P',handles.val.pressu
re_in*10^2,'water')>0
errordlg('You have not subcooled water, it will not work. Increase
pressure','Error','on')
return;
end
end
if
(get(handles.search_power,'Value')==get(handles.search_power,'Min'))&&(get(
handles.search_effic,'Value')==get(handles.search_effic,'Min'))
errordlg('Choose what you want to find','Error','on')
return
end
maxval(1) = get(handles.pentane,'Value');
amne(1)={'pentane'};%{'cyclopen'};
maxval(2) = get(handles.butane,'Value'); amne(2)={'butane'};
68
maxval(3) = get(handles.R227ea,'Value'); amne(3)={'R227ea'};
maxval(4) = get(handles.ammonia,'Value'); amne(4)={'ammonia'};
maxval(5) = get(handles.R134a,'Value');
amne(5)={'R134a'};
maxval(6) = get(handles.R114,'Value');
amne(6)={'R114'};
maxval(7) = get(handles.R245fa,'Value');
amne(7)={'R245fa'};
maxval(8) = get(handles.R113,'Value');
amne(8)={'R113'};
maxval(9) = get(handles.R123,'Value');
amne(9)={'R123'};
maxval(10) = get(handles.R141b,'Value');
amne(10)={'R141b'};
maxval(11) = get(handles.isopentane,'Value');
amne(11)={'ipentane'};
maxval(12) = get(handles.cyc_pentane,'Value');
amne(12)={'cyclopen'};
plats = 1;
for u = 1:1:length(maxval)
if maxval(u)==1
medie(plats)=amne(u);
plats = plats+1;
end
end
if plats-1<1
errordlg('You must set a substance/substances','Error','on')
set(handles.uipanel13,'BackgroundColor','red')
return
end
if (get(handles.water_heat,'Value')==get(handles.water_heat,'Max'))
P_heat_water = handles.val.pressure_in*10^2; %kPa
end
P =
[handles.val.start_pressure:handles.val.steps:handles.val.end_pressure];
m_heat = handles.val.massflow;
thigh_heat = handles.val.temperature_heat+273.15;
efficturbine = handles.val.effic_t/100;
efficpump = handles.val.effic_p/100;
if (get(handles.default_val,'Value')==get(handles.default_val,'Max'))
effic_reheat = 0.8;
else
effic_reheat = handles.val.effic_reheat/100;
end
t_overheat = handles.val.overheat;
if (get(handles.water_cool,'Value')==get(handles.water_cool,'Max'))
if(get(handles.default_temp_in,'Value')==
get(handles.default_temp_in,'Max'))
coolt = 10;
else
coolt = handles.val.temp_coolt;
end
end
if (get(handles.air_cool,'Value')==get(handles.air_cool,'Max'))
if(get(handles.default_temp_in,'Value')==
get(handles.default_temp_in,'Max'))
69
coolt = 25;
else
coolt = handles.val.temp_coolt;
end
end
t_ambient = handles.val.ambient;
tin_cool = 273.15+coolt;
Wout_vek = zeros(length(P),length(medie));
m_vek = zeros(length(P),length(medie));
wout_vek = zeros(length(P),length(medie));
Wout_ok_vek = zeros(length(P),length(medie));
effic_vek = zeros(length(P),length(medie));
Wout_ok_vek = zeros(length(P),length(medie));
effic_ok = zeros(length(P),length(medie));
warn = zeros(length(P),length(medie));
%%%%%%%%%%%%%%%%%%%%%%%%%Pressuredrop
HEX%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
if (get(handles.default_val,'Value')==get(handles.default_val,'Max'))
p_drop = 0.05; % 5% från Thern
else
p_drop=handles.val.pressure_drop/100;
end
if effic_reheat==0
%Subcritical
p23_drop = 1;
p37_drop = p23_drop*(1-p_drop);
p78_drop = p37_drop*(1-p_drop);
p84_drop = p78_drop*(1-p_drop);
%Supercritical
p23_drop_ok = 1;
p34_drop_ok = p23_drop_ok*(1-p_drop);
else
%Subcritical
p23_drop = (1-p_drop);
p37_drop = p23_drop*(1-p_drop);
p78_drop = p37_drop*(1-p_drop);
p84_drop = p78_drop*(1-p_drop);
%Supercritical
p23_drop_ok = (1-p_drop);
p34_drop_ok = p23_drop_ok*(1-p_drop);
end
%%%%%%%%%%%%%%%%%%%%%%Pinch-points%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
if (get(handles.default_val,'Value')==get(handles.default_val,'Max'))
pinch = 10; %degrees C
else
pinch = handles.val.pp_preheater;
end
if (get(handles.default_val,'Value')==get(handles.default_val,'Max'))
pinch_cond = 2;
else
pinch_cond = handles.val.pp_cond;
70
end
if (get(handles.default_val,'Value')==get(handles.default_val,'Max'))
temp_rise_coolt = 10;
else
temp_rise_coolt = handles.val.temp_rise_coolt;
end
pinch_thigh_tf4_ok = 25; %for supercritical. Temp diff between hot medie in
and fluid out
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
for j=1:length(medie)
%Reset values to avoid and leftovers that corrupt result
T = 0;
sl = 0;
sv = 0;
hf1 = 0;
tf1=0; sf1=0; Qfv=0; tfafv_heat=0;
hf2 = 0;
tf2=0; sf2=0; Qfa=0; tut_kyl=0;
hf3 = 0;
tf3=0; sf3=0; Qoh=0;
hf4 = 0;
tf4=0; sf4=0; sf2s=0;
hf5 = 0;
tf5=0; sf5=0; sf5s=0; hf5s=0;
hf6 = 0;
tf6=0; sf6=0; tf5s=0;
hf7 = 0;
tf7=0; sf7=0; tf2s=0;
hf8 = 0;
tf8=0; sf8=0;
hf9 = 0;
tf9=0; sf9=0;
hf2_ok
hf3_ok
hf4_ok
hf5_ok
hf6_ok
hf9_ok
=
=
=
=
=
=
0;
0;
0;
0;
0;
0;
sf2_ok=0;
sf3_ok=0;
sf4_ok=0;
sf5_ok=0;
sf6_ok=0;
sf9_ok=0;
tf2_ok
tf3_ok
tf4_ok
tf5_ok
tf6_ok
tf9_ok
=
=
=
=
=
=
0;
0;
0;
0;
0;
0;
tf1 = tin_cool+pinch_cond+temp_rise_coolt ;
P_cond = refpropm('P','T',tf1,'Q',0,char(medie(j)));
hf1 = refpropm('H','P',P_cond,'Q',0,char(medie(j))); %J/kg
sf1 = refpropm('S','P',P_cond,'Q',0,char(medie(j))); %J/kgK
%%%%%% Limits the condensor pressure to a minimum off 10kPa or higher
%%%
if P_cond<10
%P_cond = refpropm('P','T',tf1,'Q',0,char(medie(j)));
P_cond=10;
hf1 = refpropm('H','T',tf1,'P',P_cond,char(medie(j))); %J/kg
sf1 = refpropm('S','T',tf1,'P',P_cond,char(medie(j))); %J/kgK
else
hf1 = refpropm('H','P',P_cond,'Q',0,char(medie(j))); %J/kg
sf1 = refpropm('S','P',P_cond,'Q',0,char(medie(j))); %J/kgK
end
for i=1:1:length(P)
P_pump = P(i)*10^2; %kPa
P_cond_vek(i,j)=P_cond;
71
P_pump_vek(i,j) = P_pump;
%if the the working pressure is lower than or equal to condensor
pressure
%its not allowed run
if P_pump<=P_cond
continue
end
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%%%%%% Subcritical
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
if P_pump<refpropm('P','C',0,'',0,char(medie(j)))
m=0;
%After pump
hf2s = refpropm('H','P',P_pump,'S',sf1,char(medie(j)));%J/kg
tf2s = refpropm('T','H',hf2s,'P',P_pump,char(medie(j)));
sf2s = sf1;
hf2 = ((hf2s-hf1)/efficpump)+hf1; %J/kg
tf2 = refpropm('T','H',hf2,'P',P_pump,char(medie(j)));
sf2 = refpropm('S','P',P_pump,'H',hf2,char(medie(j)));
%If saturation temperature higher than heat source in, its not
allowed run
if refpropm('T','P',P_pump,'Q',0,char(medie(j)))<thigh_heat
count = 1;
change_p_drop=1;
while change_p_drop>0 && count<3
if count==1 && effic_reheat>0
change_p_drop = 0;
end
if change_p_drop==1 && count==2
p23_drop = 1;
p37_drop = p23_drop*(1-p_drop);
p78_drop = p37_drop*(1-p_drop);
p84_drop = p78_drop*(1-p_drop);
else
%Subcritical
p23_drop = (1-p_drop);
p37_drop = p23_drop*(1-p_drop);
p78_drop = p37_drop*(1-p_drop);
p84_drop = p78_drop*(1-p_drop);
end
%After preheater
hf7 =
refpropm('H','P',P_pump*p37_drop,'Q',0,char(medie(j)));
tf7 =
refpropm('T','P',P_pump*p37_drop,'Q',0,char(medie(j)));
72
sf7 =
refpropm('S','P',P_pump*p37_drop,'Q',0,char(medie(j)));
%After evaporator
hf8 =
refpropm('H','P',P_pump*p78_drop,'Q',1,char(medie(j)));%J/kg
tf8 =
refpropm('T','P',P_pump*p78_drop,'Q',1,char(medie(j)));
sf8 =
refpropm('S','P',P_pump*p78_drop,'Q',1,char(medie(j)));
%After superheater
if t_overheat ==0;
tf4=tf8;
else
tf4 = tf8+t_overheat;
%tf4 = thigh_heat-t_overheat;
end
if strcmp(char(medie(j)),'R245fa') && tf4>440
break;
end
if strcmp(char(medie(j)),'R134a') && tf4>455
break;
end
if strcmp(char(medie(j)),'R227ea') && tf4>475
break;
end
if strcmp(char(medie(j)),'ipentane') && tf4>500
break;
end
if strcmp(char(medie(j)),'R141b') && tf4>500
break;
end
if strcmp(char(medie(j)),'R114') && tf4>507
break;
end
if strcmp(char(medie(j)),'R113') && tf4>525
break;
end
if strcmp(char(medie(j)),'butane') && tf4>575
break;
end
if strcmp(char(medie(j)),'R123') && tf4>599
break;
end
if strcmp(char(medie(j)),'pentane') && tf4>600
break;
end
if strcmp(char(medie(j)),'cyclopen') && tf4>600
break;
end
if strcmp(char(medie(j)),'ammonia') && tf4>700
break;
end
%If tf4 = tf8 no superheater is to be used which means
that the
%pressure drop from the superheater is not to be
included.
73
if tf4 ==
refpropm('T','P',P_pump*p78_drop,'Q',1,char(medie(j)))
hf4 =
refpropm('H','P',P_pump*p78_drop,'Q',1,char(medie(j)));
sf4 =
refpropm('S','P',P_pump*p78_drop,'Q',1,char(medie(j)));
else
hf4 =
refpropm('H','T',tf4,'P',P_pump*p84_drop,char(medie(j)));
sf4 =
refpropm('S','T',tf4,'P',P_pump*p84_drop,char(medie(j)));
end
if tf4>thigh_heat
break
end
%After turbine
hf5s = refpropm('H','P',P_cond,'S',sf4,char(medie(j)));
%J/kg
sf5s = sf4;
hf5 = hf4-efficturbine*(hf4-hf5s);
sf5 = refpropm('S','P',P_cond,'H',hf5,char(medie(j)));
tf5 = refpropm('T','P',P_cond,'H',hf5,char(medie(j)));
tf5s =
refpropm('T','P',P_cond,'H',hf5s,char(medie(j)));
%Check for moisture. No reheater if moist beacuse you
are in the
%saturated area.
x = refpropm('Q','P', P_cond,'H',hf5,char(medie(j)));
x_vek(i,j)=x;
%Needed to be able to plot and calculate if in the
saturated area.
if x>0 &&
hf6 =
tf6 =
sf6 =
x<1
hf5;
tf5;
sf5;
hf3 = hf2;
tf3=tf2;
sf3 = sf2;
hf9 = hf6;
tf9 = tf6;
sf9 = sf6;
change_p_drop = 1;
else
change_p_drop = 0;
hf6 =
refpropm('H','P',P_cond,'Q',1,char(medie(j)));
74
tf6 =
refpropm('T','P',P_cond,'Q',1,char(medie(j)));
sf6 =
refpropm('S','P',P_cond,'Q',1,char(medie(j)));
h_min_reheater =
refpropm('h','t',tf2,'P',P_cond,char(medie(j)));
%Can't heatexchange down to condensation
temperature if
%efficeny of the reheater is less than 100%
hf9 = hf5-((hf5-h_min_reheater)*effic_reheat);
%Formel 15-14 värmeöverföring Sunden
tf9 =
refpropm('T','P',P_cond,'H',hf9,char(medie(j)));
sf9 =
refpropm('S','P',P_cond,'H',hf9,char(medie(j)));
%After reheater
hf3 = hf5-hf9+hf2;
tf3 =
refpropm('T','P',P_pump*p23_drop,'H',hf3,char(medie(j)));
sf3 =
refpropm('S','P',P_pump*p23_drop,'H',hf3,char(medie(j)));
prheat_gone = 0;
if tf3>=tf7
prheat_gone=1;
end
end
count=count+1;
end
%fafv= between preheater & evaporator.
tfafv_heat = tf7+pinch; %temp between preheater &
evaporator of oil/water
%Eliminates negative massflows that occurs if tfafv>thigh
and sets
%m=0 so it dosen't corrupt the results.
if tfafv_heat<thigh_heat
if
(get(handles.oil_heat,'Value')==get(handles.oil_heat,'Max'))
m = m_heat*h_diff(thigh_heat-273.15,tfafv_heat273.15)/(hf4-hf7);
else if
(get(handles.water_heat,'Value')==get(handles.water_heat,'Max'))
m=
m_heat*(refpropm('H','T',thigh_heat,'P',P_heat_water,'water')-...
refpropm('H','T',tfafv_heat,'P',P_heat_water,'water'))/(hf4-hf7);
end
end
else
m=0;
end
qtot = (m/m_heat)*(hf4-hf3);
qfv = (m/m_heat)*(hf7-hf3);
75
if
(get(handles.oil_heat,'Value')==get(handles.oil_heat,'Max'))
tlow_heat = oil_source(thigh_heat-273.15,qtot)+273.15;
else if
(get(handles.water_heat,'Value')==get(handles.water_heat,'Max'))
tlow_heat =
water_source(thigh_heat,qtot,P_heat_water);
end
end
pinch_vek(i,j)=pinch;
if (tlow_heat-5)<tf3
pinch_ny = 10;
while (tlow_heat-5-tf3)<0
tfafv_heat = tf7+pinch_ny;
if tfafv_heat<thigh_heat
if
(get(handles.oil_heat,'Value')==get(handles.oil_heat,'Max'))
m = m_heat*h_diff(thigh_heat273.15,tfafv_heat-273.15)/(hf4-hf7);
else if
(get(handles.water_heat,'Value')==get(handles.water_heat,'Max'))
m=
m_heat*(refpropm('H','T',thigh_heat,'P',P_heat_water,'water')-...
refpropm('H','T',tfafv_heat,'P',P_heat_water,'water'))/(hf4-hf7);
end
end
end
qtot = (m/m_heat)*(hf4-hf3);
if
(get(handles.oil_heat,'Value')==get(handles.oil_heat,'Max'))
tlow_heat = oil_source(thigh_heat273.15,qtot)+273.15;
else if
(get(handles.water_heat,'Value')==get(handles.water_heat,'Max'))
tlow_heat =
water_source(thigh_heat,qtot,P_heat_water);
end
end
pinch_ny = pinch_ny+1;
end
warn(i,j) = 1;
pinch_vek(i,j)=pinch_ny;
tfafv_heat = tf7+pinch_ny;
end
Qcond_kyl = m*(hf6-hf1);
tcond_kyl = tin_cool+temp_rise_coolt;
%Pressure on cooling water set to 5 bar and air to ambient
pressure
if
(get(handles.water_cool,'Value')==get(handles.water_cool,'Max'))
m_kyl=Qcond_kyl/(refpropm('H','T',tcond_kyl,'P',5*10^2,'water')-...
76
refpropm('H','T',tin_cool,'P',5*10^2,'water'));
qkyl = m*(hf9-hf1)/m_kyl;
hcool_out =
refpropm('H','T',tin_cool,'P',5*10^2,'water')+ m*(hf9-hf1)/m_kyl;
%tout_cool = water_cond(tin_cool,qkyl,5*10^2);
tout_cool =
refpropm('T','H',hcool_out,'P',5*10^2,'water');
end
if
(get(handles.air_cool,'Value')==get(handles.air_cool,'Max'))
m_kyl =
Qcond_kyl/(refpropm('H','T',tcond_kyl,'P',101,'air.ppf')-...
refpropm('H','T',tin_cool,'P',101,'air.ppf'));
density_air =
refpropm('H','T',(tin_cool+tut_kyl)/2,'P',101,'air.ppf');
Volume_flow_air = density_air/m_kyl;
qkyl = m*(hf9-hf1)/m_kyl;
hcool_out =
refpropm('H','T',tin_cool,'P',101,'air.ppf')+ m*(hf9-hf1)/m_kyl;
%tout_cool = air_cond(tin_cool,qkyl,101);
tout_cool =
refpropm('T','H',hcool_out,'P',101,'air.ppf');
end
Qkyl = m*(hf9-hf1);
Qfv = m*(hf7-hf3);
Qfa = m*(hf8-hf7);
Qoh = m*(hf4-hf8);
Qtot = Qfv+Qfa+Qoh;
Qreheat = m*(hf5-hf6);
%%%Temperature and Cp unknown and need to be
iterated%%%%%%%%%%%%%
qoh = (m/m_heat)*(hf4-hf8);
if
(get(handles.oil_heat,'Value')==get(handles.oil_heat,'Max'))
tohfa_heat = oil_source(thigh_heat-273.15,qoh)+273.15;
else if
(get(handles.water_heat,'Value')==get(handles.water_heat,'Max'))
tohfa_heat =
water_source(thigh_heat,qoh,P_heat_water);
end
end
if
(get(handles.oil_heat,'Value')==get(handles.oil_heat,'Max'))
Qoil = m_heat*h_diff(thigh_heat-273.15,tlow_heat273.15);
else if
(get(handles.water_heat,'Value')==get(handles.water_heat,'Max'))
Qoil =
m_heat*(refpropm('H','T',thigh_heat,'P',P_heat_water,'water')-...
refpropm('H','T',tlow_heat,'P',P_heat_water,'water'));
end
end
Qreheat = m*(hf5-hf6);
77
qmax_transf = h_diff(thigh_heat-273.15,t_ambient);
%%%%%%%%%%%%%%%%%%%%%%%%Performance%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%
Wout = m*(hf4-hf5); %J/kg
Win = m*(hf2-hf1);
Qin = m*(hf4-hf3); %J/kg
effic = (Wout-Win)/Qin;
effic_tot = (Wout-Win)/(m_heat*qmax_transf);
else
break %If the substance don't fulfill the condition it
starts on the
%next substance
%%%%%%%%%%%%%% End of if statement checking saturation temp
%%%%%%%%%%%%%%
end
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%%%%%%%%%Volymflöden%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%
Df4 =
refpropm('D','T',tf4,'P',P2*10^2,char(medie(j)));
%
Vf4 = m/Df4;
%
Df6 =
refpropm('D','T',tf6,'P',P_kond,char(medie(j)));
%
Vf6 = m/Df6;
%%%%%%%%%%%%%%%%%%%% Vectorizes usefull data
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
hf1_vek(i,j) = hf1;
tf1_vek(i,j) = tf1;
sf1_vek(i,j) = sf1;
hf2s_vek(i,j) = hf2s;
tf2s_vek(i,j) = tf2s;
sf2s_vek(i,j) = sf2s;
hf2_vek(i,j) = hf2;
tf2_vek(i,j) = tf2;
sf2_vek(i,j) = sf2;
hf7_vek(i,j) = hf7;
tf7_vek(i,j) = tf7;
sf7_vek(i,j) = sf7;
hf8_vek(i,j) = hf8;
tf8_vek(i,j) = tf8;
sf8_vek(i,j) = sf8;
hf4_vek(i,j) = hf4;
tf4_vek(i,j) = tf4;
sf4_vek(i,j) = sf4;
hf5s_vek(i,j) = hf5s;
tf5s_vek(i,j) = tf5s;
sf5s_vek(i,j) = sf5s;
hf5_vek(i,j) = hf5;
tf5_vek(i,j) = tf5;
78
sf5_vek(i,j)
hf6_vek(i,j)
tf6_vek(i,j)
sf6_vek(i,j)
hf3_vek(i,j)
tf3_vek(i,j)
sf3_vek(i,j)
hf9_vek(i,j)
tf9_vek(i,j)
sf9_vek(i,j)
=
=
=
=
=
=
=
=
=
=
sf5;
hf6;
tf6;
sf6;
hf3;
tf3;
sf3;
hf9;
tf9;
sf9;
tfafv_heat_vek(i,j) = tfafv_heat;
tlow_heat_vek(i,j) = tlow_heat;
tohfa_heat_vek(i,j) = tohfa_heat;
tout_cool_vek(i,j) = tout_cool;
m_vek(i,j) = m;
m_kyl_vek(i,j) = m_kyl;
%tut_kyl(i,j) = tut_kyl;
Qfv_vek(i,j) = Qfv;
Qfa_vek(i,j) = Qfa;
Qoh_vek(i,j) = Qoh;
Qtot_vek(i,j) = Qtot;
Qoil_vek(i,j) = Qoil;
Qkyl_vek(i,j) = Qkyl;
Wout_vek(i,j) = Wout; %kW
effic_vek(i,j) = effic;
effic_tot_vek(i,j)=effic_tot;
x_vek(i,j) = x;
change(i,j) = change_p_drop;
end
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%%%%%%% End of subcritical
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%%%%%%% Supercritical
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%if
P_pump*p34_drop_ok>=refpropm('P','C',0,'',0,char(medie(j)))
if P_pump*p34_drop_ok>=refpropm('P','C',0,'',0,char(medie(j))) &&
refpropm('T','C',0,'',0,char(medie(j)))<(thigh_heat-pinch_thigh_tf4_ok)
tlow_heat = 0;
%After pump
hf2s_ok = refpropm('H','P',P_pump,'S',sf1,char(medie(j)));%J/kg
tf2s_ok = refpropm('T','H',hf2s_ok,'P',P_pump,char(medie(j)));
sf2s_ok = sf1;
hf2_ok = ((hf2s_ok-hf1)/efficpump)+hf1; %J/kg
tf2_ok = refpropm('T','H',hf2_ok,'P',P_pump,char(medie(j)));
sf2_ok = refpropm('S','P',P_pump,'H',hf2_ok,char(medie(j)));
79
tf4_ok = thigh_heat-pinch_thigh_tf4_ok;
%Needs to fulfill the conditions before continuing:
if strcmp(char(medie(j)),'R245fa') && tf4>440
break;
end
if strcmp(char(medie(j)),'R134a') && tf4>455
break;
end
if strcmp(char(medie(j)),'R227ea') && tf4>475
break;
end
if strcmp(char(medie(j)),'ipentane') && tf4>500
break;
end
if strcmp(char(medie(j)),'R141b') && tf4>500
break;
end
if strcmp(char(medie(j)),'R114') && tf4>507
break;
end
if strcmp(char(medie(j)),'R113') && tf4>525
break;
end
if strcmp(char(medie(j)),'butane') && tf4>575
break;
end
if strcmp(char(medie(j)),'R123') && tf4>599
break;
end
if strcmp(char(medie(j)),'pentane') && tf4>600
break;
end
if strcmp(char(medie(j)),'cyclopen') && tf4>600
break;
end
if strcmp(char(medie(j)),'ammonia') && tf4>700
break;
end
hf4_ok =
refpropm('H','T',tf4_ok,'P',P_pump*p34_drop_ok,char(medie(j)));
sf4_ok =
refpropm('S','T',tf4_ok,'P',P_pump*p34_drop_ok,char(medie(j)));
sf5s_ok = sf4_ok;
hf5s_ok = refpropm('H','P',P_cond,'S',sf5s_ok,char(medie(j)));
tf5s_ok = refpropm('T','P',P_cond,'H',hf5s_ok,char(medie(j)));
hf5_ok = hf4_ok - efficturbine*(hf4_ok-hf5s_ok);
sf5_ok = refpropm('S','P',P_cond,'H',hf5_ok,char(medie(j)));
tf5_ok = refpropm('T','P',P_cond,'H',hf5_ok,char(medie(j)));
%Check for moisture. No reheater if moist beacuse you are in
the
%saturated area.
x = refpropm('Q','P', P_cond,'H',hf5_ok,char(medie(j)));
x_vek_ok(i,j) = x;
if x>0 && x<1
hf6_ok = hf5_ok;
80
tf6_ok = tf5_ok;
sf6_ok = sf5_ok;
hf3_ok = hf2_ok;
tf3_ok=tf2_ok;
sf3_ok = sf2_ok;
hf9_ok = hf6_ok;
tf9_ok = tf6_ok;
sf9_ok = sf6_ok;
else
hf6_ok = refpropm('H','P',P_cond,'Q',1,char(medie(j)));
tf6_ok =
refpropm('T','H',hf6_ok,'P',P_cond,char(medie(j)));
sf6_ok =
refpropm('S','H',hf6_ok,'P',P_cond,char(medie(j)));
%Can't heatexchange down to condensation temperature if
%efficeny of the reheater is less than 100%
hf9_ok = hf5_ok-(hf5_ok-hf6_ok)*effic_reheat; %Formel 15-14
värmeöverföring Sunden
tf9_ok =
refpropm('T','P',P_cond,'H',hf9_ok,char(medie(j)));
sf9_ok =
refpropm('S','P',P_cond,'H',hf9_ok,char(medie(j)));
%After reheater
hf3_ok = hf5_ok-hf9_ok+hf2_ok;
tf3_ok =
refpropm('T','P',P_pump*p23_drop,'H',hf3_ok,char(medie(j)));
sf3_ok =
refpropm('S','P',P_pump*p23_drop,'H',hf3_ok,char(medie(j)));
end
%Reset vectors to avoid faults in the iteration
Qheat_ok_vek=0;
qheat_ok_vek=0;
theat_vek=0;
Q=0;
t=0;
h=0;
%Start values
tempdiff_cold = 11; %setting a temperature to guess m
tlow_heat = tf3_ok+tempdiff_cold;
if (get(handles.oil_heat,'Value')==get(handles.oil_heat,'Max'))
m_ref = m_heat*h_diff(thigh_heat-273.15,tlow_heat273.15)/(hf4_ok-hf3_ok);
end
if
(get(handles.water_heat,'Value')==get(handles.water_heat,'Max'))
m_ref =
m_heat*(refpropm('H','T',thigh_heat,'P',P_heat_water,'water')-...
refpropm('H','T',tlow_heat,'P',P_heat_water,'water'))/(hf4_ok-hf3_ok);
end
h = [hf3_ok:100:hf4_ok];
P_3=P_pump*p23_drop_ok;
P_4 = P_pump*p34_drop_ok;
P_drop_point = (P_3-P_4)/length(h);
81
dpp_dm = 0;
pp = 100;
raknare = 0;
whilerak=0;
m=m_ref;
while abs(pinch-pp)>0.1
m = m-dpp_dm;
for l=1:1:length(h)
Q(l) = m*(h(l)-h(1));
t(l) = refpropm('T','P',P_3P_drop_point*l,'H',h(l),char(medie(j)));
end
raknare = 0;
for o=length(h):-1:1
Qheat = Q(length(h)-o+1);
Qheat_vek(o) = Qheat;
qheat = Qheat/m_heat;
qheat_vek(o)= qheat;
end
q2 = 0;
if
(get(handles.oil_heat,'Value')==get(handles.oil_heat,'Max'))
theat = thigh_heat-273.15;
for l=length(h):-1:1
qheat = qheat_vek(l)-q2;
theat = oil_source(theat,qheat); %See fkn file
oil_source
theat_vek(l)=theat+273.15;
q2 = qheat_vek(l);
raknare = raknare+1;
end
end
if
(get(handles.water_heat,'Value')==get(handles.water_heat,'Max'))
theat = thigh_heat;
for l=length(h):-1:1
qheat = qheat_vek(l)-q2;
theat = water_source(theat,qheat,P_heat_water);
%See fkn file water_source
theat_vek(l)=theat;
q2 = qheat_vek(l);
raknare = raknare+1;
end
end
whilerak=whilerak+1
m_while(whilerak)=m;
tdiff = theat_vek-t;
pp = min(tdiff);
pp_vek(whilerak) = pp;
dpp_dm = (pinch-pp)/m;
82
end
tlow_heat = theat_vek(1);
Qcond_kyl_ok = m*(hf6_ok-hf1);
tcond_kyl = tin_cool+temp_rise_coolt;
if
(get(handles.water_cool,'Value')==get(handles.water_cool,'Max'))
m_kyl=Qcond_kyl_ok/(refpropm('H','T',tcond_kyl,'P',5*10^2,'water')-...
refpropm('H','T',tin_cool,'P',5*10^2,'water'));
qkyl = m*(hf9_ok-hf1)/m_kyl;
tout_cool = water_cond(tin_cool,qkyl,5*10^2);
end
if (get(handles.air_cool,'Value')==get(handles.air_cool,'Max'))
m_kyl =
Qcond_kyl_ok/(refpropm('H','T',tcond_kyl,'P',101,'air.ppf')-...
refpropm('H','T',tin_cool,'P',101,'air.ppf'));
density_air =
refpropm('H','T',(tin_cool+tut_kyl)/2,'P',101,'air.ppf');
Volume_flow_air = density_air/m_kyl;
qkyl = m*(hf9_ok-hf1)/m_kyl;
tout_cool = air_cond(tin_cool,qkyl,101);
end
qmax_transf_ok = h_diff(thigh_heat,t_ambient);
Qkyl_ok = m*(hf9_ok-hf1);
y =find(tdiff==pp);
theat_pp = theat_vek(y);
tf_pp = t(y);
Q_pp = Q(y);
tt = [theat_pp tf_pp];
en = [Q_pp Q_pp];
Wout_ok = m*(hf4_ok-hf5_ok);
Win_ok = m*(hf2_ok-hf1);
Qin_ok = m_heat*h_diff(thigh_heat,tlow_heat);
effic_ok(i,j) = (Wout_ok-Win_ok)/Qin_ok;
effic_tot_ok(i,j) = (Wout_ok-Win_ok)/(m_heat*qmax_transf_ok);
m_kyl_ok_vek(i,j) = m_kyl;
m_ok_vek(i,j) = m;
Wout_ok_vek(i,j)=Wout_ok;
tlow_ok_vek(i,j)= tlow_heat;
tout_cool_ok(i,j) = tout_cool;
Qkyl_ok_vek(i,j) = Qkyl_ok;
hf1_ok_vek(i,j) = hf1;
sf1_ok_vek(i,j) = sf1;
tf2_ok_vek(i,j) = tf2_ok;
hf2s_ok_vek(i,j) = hf2s_ok;
sf2s_ok_vek(i,j) = sf2s_ok;
tf3_ok_vek(i,j) = tf3_ok;
hf4_ok_vek(i,j) = hf4_ok;
sf4_ok_vek(i,j) = sf4_ok;
tf5_ok_vek(i,j) = tf5_ok;
hf5s_ok_vek(i,j) = hf5s_ok;
83
tf1_ok_vek(i,j) = tf1;
hf2_ok_vek(i,j) = hf2_ok;
sf2_ok_vek(i,j) = sf2_ok;
tf2s_ok_vek(i,j) = tf2s_ok;
hf3_ok_vek(i,j) = hf3_ok;
sf3_ok_vek(i,j) = sf3_ok;
tf4_ok_vek(i,j) = tf4_ok;
hf5_ok_vek(i,j) = hf5_ok;
sf5_ok_vek(i,j) = sf5_ok;
tf5s_ok_vek(i,j) = tf5s_ok;
sf5s_ok_vek(i,j) = sf5s_ok;
tf6_ok_vek(i,j) = tf6_ok;
hf9_ok_vek(i,j) = hf9_ok;
sf9_ok_vek(i,j) = sf9_ok;
hf6_ok_vek(i,j) = hf6_ok;
sf6_ok_vek(i,j) = sf6_ok;
tf9_ok_vek(i,j) = tf9_ok;
end
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%%%%%%%% End Supercritical
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%% End of for loop on pressure
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
end
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%% End of for loop on medie
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
end
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%%%%%%% Find Best %%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
W_ok_uk =Wout_vek+Wout_ok_vek;
effic_ok_uk = effic_vek+effic_ok;
if (get(handles.search_power,'Value')==get(handles.search_power,'Max'))
max_effekt = 0;
koll_effekt = 0;
koll_effic=0;
for u=1:length(P)
for k=1:length(medie)
effekt = W_ok_uk(u,k);
if effekt>max_effekt
max_effekt = effekt;
rad=u;
col=k;
koll_effekt=koll_effekt+1;
end
end
end
end
if (get(handles.search_effic,'Value')==get(handles.search_effic,'Max'))
koll_effic=0;
max_effic = 0;
koll_effekt = 0;
for u = 1:length(P)
for k=1:length(medie)
effic = effic_ok_uk(u,k);
if effic>max_effic
max_effic=effic;
rad = u;
col = k;
koll_effic=koll_effic+1;
84
end
end
end
end
if koll_effic==0 && koll_effekt==0
errordlg('Can not calculate for choosen substance/substances.
Temperature might be to low alt. pressure to high','Error','on')
end
%for the plot of saturation curve
if strcmp(medie(col),'R114')
range=(33:refpropm('P','C',0,'',0,char(medie(col)))-10);
else
range=(33:refpropm('P','C',0,'',0,char(medie(col)))-2);
end
nsat=0;
for o=1:length(range)
nsat=nsat+1;
T(nsat)=refpropm('T','P',range(o),'Q',0,char(medie(col)));
sl(nsat)=refpropm('S','P',range(o),'Q',0,char(medie(col)));
sv(nsat)=refpropm('S','P',range(o),'Q',1,char(medie(col)));
end
T(nsat+1)= refpropm('T','C',0,'',0,char(medie(col)));
sl(nsat+1)=refpropm('S','C',0,'',0,char(medie(col)));
sv(nsat+1)=refpropm('S','C',0,'',0,char(medie(col)));
%%%%%%%%%%%%%%%%%%%%%%%%%% Sub critical %%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
if P(rad)*10^2<refpropm('P','C',0,'',0,char(medie(col)))
t1 = tf1_vek(rad,col);
s1 = sf1_vek(rad,col);
t2s = tf2s_vek(rad,col);
s2s=sf2s_vek(rad,col);
t2 = tf2_vek(rad,col);
s2 = sf2_vek(rad,col);
t3 = tf3_vek(rad,col);
s3 = sf3_vek(rad,col);
t4 = tf4_vek(rad,col);
s4 = sf4_vek(rad,col);
t5s = tf5s_vek(rad,col);
s5s=sf5s_vek(rad,col);
t5 = tf5_vek(rad,col);
s5 = sf5_vek(rad,col);
t6 = tf6_vek(rad,col);
s6 = sf6_vek(rad,col);
t7 = tf7_vek(rad,col);
s7 = sf7_vek(rad,col);
t8 = tf8_vek(rad,col);
s8 = sf8_vek(rad,col);
t9 = tf9_vek(rad,col);
s9 = sf9_vek(rad,col);
Tm = (hf4_vek(rad,col)-hf3_vek(rad,col))/(sf4_vek(rad,col)sf3_vek(rad,col))-273.15;
if warn(rad,col)==1
warndlg('Pinchpoint has changed to lower the mass to be boiled. See
new pinchpoint preheater in result','Trying to boil to much mass');
set(handles.pp_new_descrip,'Visible','on');
set(handles.pp_new,'Visible','on');
set(handles.pp_new_unit,'Visible','on');
set(handles.pp_new,'String',pinch_vek(rad,col))
end
t12s =[t1 t2s]; s12s = [s1 s2s];
t12 = [t1 t2]; s12 = [s1 s2];
t23 = [t2s t3]; s23 = [s2s s3];
t37 = [t3 t7]; s37 = [s3 s7];
t78 = [t7 t8]; s78 = [s7 s8];
t84 = [t8 t4]; s84 = [s8 s4];
t45s =[t4 t5s]; s45s = [s4 s5s];
85
t45
t59
t96
t61
t53
t92
=
=
=
=
=
=
[t4
[t5
[t9
[t6
[t5
[t9
t5];
t9];
t6];
t1];
t3];
t2];
s45
s59
s96
s61
s53
s92
=
=
=
=
=
=
[s4
[s5
[s9
[s6
[s5
[s9
s5];
s9];
s6];
s1];
s3];
s2];
if t4>=thigh_heat
errordlg('your superheating are to high, lower
this','Error','on')
end
hold on
plot(handles.T_s,sl,T,'r-','linesmoothing','on')
plot(handles.T_s,sv,T,'r-','linesmoothing','on')
title(handles.T_s,'T-s diagram')
ylabel(handles.T_s,'T(K)')
xlabel(handles.T_s,'s (J/kgK)')
plot(handles.T_s,s12s,t12s,'b--')
plot(handles.T_s,s12,t12,'b-')
plot(handles.T_s,s23,t23,'b-','Linewidth',1.5,'linesmoothing','on')
plot(handles.T_s,s37,t37,'b-','Linewidth',1.5,'linesmoothing','on')
plot(handles.T_s,s78,t78,'b-','Linewidth',1.5,'linesmoothing','on')
plot(handles.T_s,s84,t84,'b-','Linewidth',1.5,'linesmoothing','on')
plot(handles.T_s,s45s,t45s,'b--','Linewidth',1.5,'linesmoothing','on')
plot(handles.T_s,s45,t45,'b-','Linewidth',1.5,'linesmoothing','on')
plot(handles.T_s,s59,t59,'b-','Linewidth',1.5,'linesmoothing','on')
plot(handles.T_s,s96,t96,'g-','Linewidth',1.5,'linesmoothing','on')
plot(handles.T_s,s61,t61,'b-','Linewidth',1.5,'linesmoothing','on')
if effic_reheat>0 && x_vek(rad,col)>=1
plot(handles.T_s,s53,t53,'r--','Linewidth',1.5,'linesmoothing','on')
plot(handles.T_s,s92,t92,'r--','Linewidth',1.5,'linesmoothing','on')
end
hold off
%T-Q
Qheatplot = [Qfv_vek(rad,col)+Qfa_vek(rad,col)+Qoh_vek(rad,col),...
Qfv_vek(rad,col)+Qfa_vek(rad,col),Qfv_vek(rad,col),0];
theatplot =
[thigh_heat,tohfa_heat_vek(rad,col),tfafv_heat_vek(rad,col),...
tlow_heat_vek(rad,col)];
tplot =
[tf4_vek(rad,col),tf8_vek(rad,col),tf7_vek(rad,col),tf3_vek(rad,col)];
hold on
title(handles.T_Q,'T-Q diagram')
ylabel(handles.T_Q,'T(K)')
xlabel(handles.T_Q,'Q(W)')
plot(handles.T_Q,Qheatplot,theatplot,'r','Linewidth',1.5,'linesmoothing','on')
plot(handles.T_Q,Qheatplot,tplot,'b','Linewidth',1.5,'linesmoothing','on')
hold off
pressure = P(rad);
set(handles.pressure,'String',pressure);
power = round(10*(W_ok_uk(rad,col)/10^3))/10;
set(handles.power,'String',power);
effic = round(10000*effic_ok_uk(rad,col))/100;
86
set(handles.effic,'String',effic);
tot_effic = round(10000*effic_tot_vek(rad,col))/100;
set(handles.tot_effic,'String',tot_effic);
substance = char(medie(col));
set(handles.substance,'String',substance);
set(handles.cycle,'String','subcritical');
mass_fluid=round(10*m_vek(rad,col))/10;
set(handles.mass_fluid,'String',mass_fluid);
set(handles.tout_heat,'String',round(10*(tlow_heat_vek(rad,col)273.15))/10)
set(handles.cool_out,'String',round(10*(tout_cool_vek(rad,col)273.15))/10)
if change(rad,col)==1;
p23_drop = 1;
p37_drop = p23_drop*(1-p_drop);
p78_drop = p37_drop*(1-p_drop);
p84_drop = p78_drop*(1-p_drop);
else
%Subcritical
p23_drop = (1-p_drop);
p37_drop = p23_drop*(1-p_drop);
p78_drop = p37_drop*(1-p_drop);
p84_drop = p78_drop*(1-p_drop);
end
if t4>t8
if effic_reheat==0 || x_vek(rad,col)<=1
figure(2)
hold on
imshow('Overheat_No_reheat.bmp');
%Heat & Cool
text(34,85,['\color[rgb]{0.745,0.294,0.282}m=',num2str(m_heat),'
kg/s'],'FontSize',8)
text(34,105,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(thigh_heat273.15)),' C'],'FontSize',8)
text(255,201,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(tohfa_heat_v
ek(rad,col)-273.15)),' C'],'FontSize',8)
text(36,309,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(tfafv_heat_ve
k(rad,col)-273.15)),' C'],'FontSize',8)
text(34,448,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(tlow_heat_vek
(rad,col)-273.15)),' C'],'FontSize',8)
text(673,735,['\color[rgb]{0.29,0.494,0.733}m=',num2str(round(10*m_kyl_vek(
rad,col))/10),' kg/s'],'FontSize',8)
text(673,755,['\color[rgb]{0.29,0.494,0.733}T=',num2str(round(tin_cool273.15)),' C'],'FontSize',8)
text(673,646,['\color[rgb]{0.29,0.494,0.733}T=',num2str(round(tout_cool_vek
(rad,col)-273.15)),' C'],'FontSize',8)
%1
text(566,810,['P=',num2str(round(P_cond_vek(rad,col))/100),'
Bar'],'FontSize',8)
87
text(566,830,['T=',num2str(round(tf1-273.15)),'
C'],'FontSize',8)
%2
text(346,637,['m=',num2str(mass_fluid),' kg/s'],'FontSize',8)
text(346,657,['P=',num2str(pressure),' Bar'],'FontSize',8)
text(346,677,['T=',num2str(round(tf2_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%4
text(299,28,['P=',num2str(round(10*pressure*p84_drop)/10),'
Bar'],'FontSize',8)
text(299,48,['T=',num2str(round(tf4_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%5
text(637,304,['P=',num2str(round(P_cond_vek(rad,col))/100),'
Bar'],'FontSize',8)
text(637,324,['T=',num2str(round(tf5_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%6
%7
text(182,330,['P=',num2str(round(10*pressure*p37_drop)/10),'
Bar'],'FontSize',8)
text(182,361,['T=',num2str(round(tf7_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%8
text(73,191,['P=',num2str(round(10*pressure*p78_drop)/10),'
Bar'],'FontSize',8)
text(73,211,['T=',num2str(round(tf8_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%Tm
text(327,271,['Tm=',num2str(round(10*Tm)/10),'
C'],'Fontsize',10)
hold off
else
figure(2)
hold on
imshow('Overheat.bmp');
%Heat & Cool
text(34,85,['\color[rgb]{0.745,0.294,0.282}m=',num2str(m_heat),'
kg/s'],'FontSize',8)
text(34,105,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(thigh_heat273.15)),' C'],'FontSize',8)
text(255,201,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(tohfa_heat_v
ek(rad,col)-273.15)),' C'],'FontSize',8)
text(36,309,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(tfafv_heat_ve
k(rad,col)-273.15)),' C'],'FontSize',8)
text(34,448,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(tlow_heat_vek
(rad,col)-273.15)),' C'],'FontSize',8)
text(673,735,['\color[rgb]{0.29,0.494,0.733}m=',num2str(round(10*m_kyl_vek(
rad,col))/10),' kg/s'],'FontSize',8)
text(673,755,['\color[rgb]{0.29,0.494,0.733}T=',num2str(round(tin_cool273.15)),' C'],'FontSize',8)
88
text(673,646,['\color[rgb]{0.29,0.494,0.733}T=',num2str(round(tout_cool_vek
(rad,col)-273.15)),' C'],'FontSize',8)
%1
text(566,810,['P=',num2str(round(P_cond_vek(rad,col))/100),'
Bar'],'FontSize',8)
text(566,830,['T=',num2str(round(tf1-273.15)),'
C'],'FontSize',8)
%2
text(342,637,['m=',num2str(mass_fluid),' kg/s'],'FontSize',8)
text(342,657,['P=',num2str(pressure),' Bar'],'FontSize',8)
text(342,677,['T=',num2str(round(tf2_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%3
text(247,507,['P=',num2str(round(10*pressure*p23_drop)/10),'
Bar'],'FontSize',8)
text(247,527,['T=',num2str(round(tf3_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%4
text(299,28,['P=',num2str(round(10*pressure*p84_drop)/10),'
Bar'],'FontSize',8)
text(299,48,['T=',num2str(round(tf4_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%5
text(637,304,['P=',num2str(round(P_cond_vek(rad,col))/100),'
Bar'],'FontSize',8)
text(637,324,['T=',num2str(round(tf5_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%6
%7
text(182,330,['P=',num2str(round(10*pressure*p37_drop)/10),'
Bar'],'FontSize',8)
text(182,361,['T=',num2str(round(tf7_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%8
text(73,191,['P=',num2str(round(10*pressure*p78_drop)/10),'
Bar'],'FontSize',8)
text(73,211,['T=',num2str(round(tf8_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%9
text(637,552,['P=',num2str(round(P_cond_vek(rad,col))/100),'
Bar'],'FontSize',8)
text(637,572,['T=',num2str(round(tf9_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%Tm
text(327,271,['Tm=',num2str(round(10*Tm)/10),'C'],'Fontsize',10)
hold off
end
end
if t4==t8
if effic_reheat==0 || x_vek(rad,col)<=1
figure(2)
hold on
imshow('Sat_No_reheat.bmp');
%Heat & Cool
text(39,82,['\color[rgb]{0.745,0.294,0.282}m=',num2str(m_heat),'
kg/s'],'FontSize',8)
89
text(39,102,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(thigh_heat273.15)),' C'],'FontSize',8)
text(228,235,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(tfafv_heat_v
ek(rad,col)-273.15)),' C'],'FontSize',8)
text(39,387,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(tlow_heat_vek
(rad,col)-273.15)),' C'],'FontSize',8)
text(641,652,['\color[rgb]{0.29,0.494,0.733}m=',num2str(round(10*m_kyl_vek(
rad,col))/10),' kg/s'],'FontSize',8)
text(641,672,['\color[rgb]{0.29,0.494,0.733}T=',num2str(round(tin_cool273.15)),' C'],'FontSize',8)
text(641,578,['\color[rgb]{0.29,0.494,0.733}T=',num2str(round(tout_cool_vek
(rad,col)-273.15)),' C'],'FontSize',8)
%1
text(568,737,['P=',num2str(round(P_cond_vek(rad,col))/100),'
Bar'],'FontSize',8)
text(568,757,['T=',num2str(round(tf1-273.15)),'
C'],'FontSize',8)
%2
text(334,518,['m=',num2str(mass_fluid),' kg/s'],'FontSize',8)
text(334,538,['P=',num2str(pressure),' Bar'],'FontSize',8)
text(334,558,['T=',num2str(round(tf2_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%4
text(305,35,['P=',num2str(round(10*pressure*p78_drop)/10),'
Bar'],'FontSize',8)
text(305,55,['T=',num2str(round(tf4_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%5
text(608,351,['P=',num2str(round(P_cond_vek(rad,col))/100),'
Bar'],'FontSize',8)
text(608,371,['T=',num2str(round(tf5_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%7
text(80,237,['P=',num2str(round(10*pressure*p37_drop)/10),'
Bar'],'FontSize',8)
text(80,257,['T=',num2str(round(tf7_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%Tm
text(327,271,['Tm=',num2str(round(10*Tm)/10),'C'],'Fontsize',10)
hold off
else
figure(2)
hold on
imshow('Saturated.bmp');
%Heat & Cool
text(34,81,['\color[rgb]{0.745,0.294,0.282}m=',num2str(m_heat),'
kg/s'],'FontSize',8)
text(34,101,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(thigh_heat273.15)),' C'],'FontSize',8)
90
text(228,235,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(tfafv_heat_v
ek(rad,col)-273.15)),' C'],'FontSize',8)
text(34,387,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(tlow_heat_vek
(rad,col)-273.15)),' C'],'FontSize',8)
text(649,660,['\color[rgb]{0.29,0.494,0.733}m=',num2str(round(10*m_kyl_vek(
rad,col))/10),' kg/s'],'FontSize',8)
text(649,680,['\color[rgb]{0.29,0.494,0.733}T=',num2str(round(tin_cool273.15)),' C'],'FontSize',8)
text(649,570,['\color[rgb]{0.29,0.494,0.733}T=',num2str(round(tout_cool_vek
(rad,col)-273.15)),' C'],'FontSize',8)
%1
text(555,738,['P=',num2str(round(P_cond_vek(rad,col))/100),'
Bar'],'FontSize',8)
text(555,758,['T=',num2str(round(tf1-273.15)),'
C'],'FontSize',8)
%2
text(344,577,['m=',num2str(mass_fluid),' kg/s'],'FontSize',8)
text(344,597,['P=',num2str(pressure),' Bar'],'FontSize',8)
text(344,617,['T=',num2str(round(tf2_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%3
text(266,438,['P=',num2str(round(10*pressure*p23_drop)/10),'
Bar'],'FontSize',8)
text(266,458,['T=',num2str(round(tf3_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%4
text(301,35,['P=',num2str(round(10*pressure*p78_drop)/10),'
Bar'],'FontSize',8)
text(301,55,['T=',num2str(round(tf4_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%5
text(613,295,['P=',num2str(round(P_cond_vek(rad,col))/100),'
Bar'],'FontSize',8)
text(613,315,['T=',num2str(round(tf5_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%7
text(80,236,['P=',num2str(round(10*pressure*p37_drop)/10),'
Bar'],'FontSize',8)
text(80,256,['T=',num2str(round(tf7_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%9
text(608,487,['P=',num2str(round(P_cond_vek(rad,col))/100),'
Bar'],'FontSize',8)
text(608,507,['T=',num2str(round(tf9_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%Tm
text(327,271,['Tm=',num2str(round(10*Tm)/10),'C'],'Fontsize',10)
hold off
end
end
savedata(1)= hf4_vek(rad,col);%h4
savedata(2)= sf4_vek(rad,col);%s4
91
savedata(3)= tf4_vek(rad,col);%t4
savedata(4)= P_pump_vek(rad,col)*p84_drop;%P4
savedata(5)= tf5_vek(rad,col);%t5
savedata(6)= hf5_vek(rad,col);%h5
savedata(7)= sf5_vek(rad,col);%s5
savedata(8)= sf5s_vek(rad,col);%s5s
savedata(9)= P_cond_vek(rad,col);%P5
savedata(10)= mass_fluid;
fluid = char(medie(col));
%global savedata
end
%%%%%%%%%%%%%%%%%%%%%%%%% Supercritical %%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
if P(rad)*10^2*p34_drop_ok>refpropm('P','C',0,'',0,char(medie(col)))
n=0;
range1 = [tf3_ok_vek(rad,col):tf4_ok_vek(rad,col)];
t34 = range1;
P_3=P_pump*p23_drop;
P_4 = P_pump*p34_drop_ok;
P_drop_point = (P_3-P_4)/length(h);
for n=1:length(range1)
s34(n) = refpropm('S','T',range1(n),'P',P_3P_drop_point,char(medie(col)));
end
n=0;
range2 = [tf2s_ok_vek(rad,col):tf3_ok_vek(rad,col)];
t23 = range2;
for n=1:length(range2)
s23(n) = refpropm('S','T',range2(n),'P',P_pump,char(medie(col)));
end
t12s =[tf1_ok_vek(rad,col) tf2s_ok_vek(rad,col)];
s12s = [sf1_ok_vek(rad,col) sf2s_ok_vek(rad,col)];
t12 = [tf1_ok_vek(rad,col) tf2_ok_vek(rad,col)];
s12 = [sf1_ok_vek(rad,col) sf2_ok_vek(rad,col)];
t45s = [tf4_ok_vek(rad,col) tf5s_ok_vek(rad,col)];
s45s= [sf4_ok_vek(rad,col) sf5s_ok_vek(rad,col)];
t45 = [tf4_ok_vek(rad,col) tf5_ok_vek(rad,col)];
s45= [sf4_ok_vek(rad,col) sf5_ok_vek(rad,col)];
t61 = [tf6_ok_vek(rad,col) tf1_ok_vek(rad,col)];
s61 = [sf6_ok_vek(rad,col) sf1_ok_vek(rad,col)];
s96 = [sf9_ok_vek(rad,col) sf6_ok_vek(rad,col)];
t96 = [tf9_ok_vek(rad,col) tf6_ok_vek(rad,col)];
s59 = [sf5_ok_vek(rad,col) sf9_ok_vek(rad,col)];
t59 = [tf5_ok_vek(rad,col) tf9_ok_vek(rad,col)];
t53 = [tf5_ok_vek(rad,col) tf3_ok_vek(rad,col)];
s53 = [sf5_ok_vek(rad,col) sf3_ok_vek(rad,col)];
t92 = [tf9_ok_vek(rad,col) tf2_ok_vek(rad,col)];
s92 = [sf9_ok_vek(rad,col) sf2_ok_vek(rad,col)];
Tm = (hf4_ok_vek(rad,col)-hf3_ok_vek(rad,col))/(sf4_ok_vek(rad,col)sf3_ok_vek(rad,col));
plot(handles.T_s,sl,T,'r-','linesmoothing','on')
plot(handles.T_s,sv,T,'r-','linesmoothing','on')
92
plot(handles.T_s,s12s,t12s,'b--','linesmoothing','on')
plot(handles.T_s,s12,t12,'b-','linesmoothing','on')
plot(handles.T_s,s23,t23,'b-','linesmoothing','on')
plot(handles.T_s,s34,t34,'b-','linesmoothing','on')
plot(handles.T_s,s45,t45,'b-','linesmoothing','on')
plot(handles.T_s,s45s,t45s,'b--','linesmoothing','on')
plot(handles.T_s,s59,t59,'b-','linesmoothing','on')
plot(handles.T_s,s96,t96,'g-','linesmoothing','on')
plot(handles.T_s,s61,t61,'b-','linesmoothing','on')
plot(handles.T_s,s92,t92,'r--','linesmoothing','on')
plot(handles.T_s,s53,t53,'r--','linesmoothing','on')
%T-Q
h = [hf3_ok_vek(rad,col):1000:hf4_ok_vek(rad,col)];
P_3=P_pump*p23_drop;
P_4 = P_pump*p34_drop_ok;
P_drop_point = (P_3-P_4)/length(h);
theat_vek = 0;
%For medie
m_bast = m_ok_vek(rad,col);
for l=1:1:length(h)
Qf(l) = m_bast*(h(l)-hf3_ok_vek(rad,col));
tf(l) = refpropm('T','P',P_3l*P_drop_point,'H',h(l),char(medie(col)));
end
for o=length(h):-1:1
Qheat = Qf(length(h)-o+1);
Qheat_vek(o) = Qheat;
qheat = Qheat/m_heat;
qheat_vek(o)= qheat;
end
%For heat source
q2 = 0;
if (get(handles.oil_heat,'Value')==get(handles.oil_heat,'Max'))
theat = thigh_heat-273.15;
for l=length(h):-1:1
qheat = qheat_vek(l)-q2;
theat = oil_source(theat,qheat); %Se fkn fil T_Q
theat_vek(l)=theat+273.15;
q2 = qheat_vek(l);
end
end
if (get(handles.water_heat,'Value')==get(handles.water_heat,'Max'))
theat = thigh_heat;
for l=length(h):-1:1
qheat = qheat_vek(l)-q2;
theat = water_source(theat,qheat,P_heat_water);
93
theat_vek(l)=theat;
q2 = qheat_vek(l);
end
end
tdiff = theat_vek-tf;
pp = min(tdiff);
y =find(tdiff==pp);
theat_pp = theat_vek(y);
tf_pp = tf(y);
Q_pp = Qf(y);
tt = [theat_pp tf_pp];
en = [Q_pp Q_pp];
hold on
plot(handles.T_Q,Qf,tf,'b-')
plot(handles.T_Q,Qf,theat_vek,'r-')
plot(handles.T_Q,en,tt,'g-')
hold off
pressure = P(rad);
set(handles.pressure,'String',pressure);
power = round(10*(W_ok_uk(rad,col)/10^3))/10;
set(handles.power,'String',power);
effic = round(10000*effic_ok_uk(rad,col))/100;
set(handles.effic,'String',effic);
substance = char(medie(col));
set(handles.substance,'String',substance);
set(handles.cycle,'String','supercritical');
mass_fluid=round(100*(m_ok_vek(rad,col)))/100;
set(handles.mass_fluid,'String',mass_fluid);
set(handles.tout_heat,'String',round(10*(tlow_ok_vek(rad,col)273.15))/10)
set(handles.cool_out,'String',round(10*(tout_cool_ok(rad,col)273.15))/10)
tot_effic = round(10000*effic_tot_ok(rad,col))/100;
set(handles.tot_effic,'String',tot_effic);
if effic_reheat==0 || x_vek_ok(rad,col)<=1
figure(2)
hold on
imshow('Supercritical_no_reheat.bmp');
%Heat & Cool
text(41,148,['\color[rgb]{0.745,0.294,0.282}m=',num2str(m_heat),'
kg/s'],'FontSize',8)
text(41,168,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(thigh_heat273.15)),' C'],'FontSize',8)
text(41,328,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(tlow_ok_vek(r
ad,col)-273.15)),' C'],'FontSize',8)
text(533,654,['\color[rgb]{0.29,0.494,0.733}m=',num2str(round(10*m_kyl_ok_v
ek(rad,col))/10),' kg/s'],'FontSize',8)
text(533,674,['\color[rgb]{0.29,0.494,0.733}T=',num2str(round(tin_cool273.15)),' C'],'FontSize',8)
94
text(533,577,['\color[rgb]{0.29,0.494,0.733}T=',num2str(round(tout_cool_ok(
rad,col)-273.15)),' C'],'FontSize',8)
%1
text(446,739,['P=',num2str(round(P_cond_vek(rad,col))/100),'
Bar'],'FontSize',8)
text(446,759,['T=',num2str(round(tf1-273.15)),' C'],'FontSize',8)
%2
text(243,552,['m=',num2str(round(10*mass_fluid)/10),'
kg/s'],'FontSize',8)
text(243,572,['P=',num2str(pressure),' Bar'],'FontSize',8)
text(243,592,['T=',num2str(round(tf2_ok_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%4
text(248,30,['P=',num2str(round(10*pressure*p34_drop_ok)/10),'
Bar'],'FontSize',8)
text(248,50,['T=',num2str(round(tf4_ok_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%5
text(502,303,['P=',num2str(round(P_cond_vek(rad,col))/100),'
Bar'],'FontSize',8)
text(502,323,['T=',num2str(round(tf5_ok_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%Tm
text(327,271,['Tm=',num2str(round(10*Tm)/10),'C'],'Fontsize',10)
hold off
else
figure(2)
hold on
imshow('Supercritical.bmp');
%Heat & Cool
text(41,148,['\color[rgb]{0.745,0.294,0.282}m=',num2str(m_heat),'
kg/s'],'FontSize',8)
text(41,168,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(thigh_heat273.15)),' C'],'FontSize',8)
text(41,328,['\color[rgb]{0.745,0.294,0.282}T=',num2str(round(tlow_ok_vek(r
ad,col)-273.15)),' C'],'FontSize',8)
text(533,654,['\color[rgb]{0.29,0.494,0.733}m=',num2str(round(10*m_kyl_ok_v
ek(rad,col))/10),' kg/s'],'FontSize',8)
text(533,674,['\color[rgb]{0.29,0.494,0.733}T=',num2str(round(tin_cool273.15)),' C'],'FontSize',8)
text(533,577,['\color[rgb]{0.29,0.494,0.733}T=',num2str(round(tout_cool_ok(
rad,col)-273.15)),' C'],'FontSize',8)
%1
text(446,739,['P=',num2str(round(P_cond_vek(rad,col))/100),'
Bar'],'FontSize',8)
text(446,759,['T=',num2str(round(tf1-273.15)),' C'],'FontSize',8)
%2
text(243,552,['m=',num2str(round(10*mass_fluid)/10),'
kg/s'],'FontSize',8)
text(243,572,['P=',num2str(pressure),' Bar'],'FontSize',8)
text(243,592,['T=',num2str(round(tf2_ok_vek(rad,col)-273.15)),'
C'],'FontSize',8)
95
%3
text(198,441,['P=',num2str(round(10*pressure*p23_drop_ok)/10),'
Bar'],'FontSize',8)
text(198,461,['T=',num2str(round(tf3_ok_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%4
text(248,30,['P=',num2str(round(10*pressure*p34_drop_ok)/10),'
Bar'],'FontSize',8)
text(248,50,['T=',num2str(round(tf4_ok_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%5
text(502,303,['P=',num2str(round(P_cond_vek(rad,col))/100),'
Bar'],'FontSize',8)
text(502,323,['T=',num2str(round(tf5_ok_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%9
text(502,471,['P=',num2str(round(P_cond_vek(rad,col))/100),'
Bar'],'FontSize',8)
text(502,491,['T=',num2str(round(tf9_ok_vek(rad,col)-273.15)),'
C'],'FontSize',8)
%Tm
text(327,271,['Tm=',num2str(round(10*Tm)/10),'C'],'Fontsize',10)
hold off
end
savedata(1)= hf4_ok_vek(rad,col);
savedata(2)= sf4_ok_vek(rad,col);
savedata(3)= tf4_ok_vek(rad,col);
savedata(4)= P_pump_vek(rad,col)*p34_drop_ok;
savedata(5)= tf5_ok_vek(rad,col);
savedata(6)= hf5_ok_vek(rad,col);
savedata(7)= sf5_ok_vek(rad,col);
savedata(8)= sf5s_ok_vek(rad,col);
savedata(9)= P_cond_vek(rad,col);
savedata(10)= mass_fluid;
fluid = char(medie(col));
end
global EXPORT_VALUES
global fluid_select
fluid_select = fluid;
EXPORT_VALUES = savedata;
set(handles.wait,'BackgroundColor','green');
set(handles.wait,'String','Done')
set(handles.Turb_calc,'Visible','on')
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%SLUT BERÄKNINGAR SAMT PLOT%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%%
% --- Executes on button press in clear.
function clear_Callback(hObject, eventdata, handles)
% hObject
handle to clear (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
cla(handles.T_s);
cla(handles.T_Q);
set(handles.effic,'String','-');
set(handles.substance,'String','-');
set(handles.cycle,'String','-');
set(handles.mass_fluid,'String','-');
96
set(handles.power,'String','-');
set(handles.pressure,'String','-');
set(handles.tout_heat,'String','-');
% --- Executes on button press in reset.
function reset_Callback(hObject, eventdata, handles)
% hObject
handle to reset (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
set(handles.wait,'BackgroundColor','white');
set(handles.wait,'String','-');
%Nollställ kylning
% minVal = get(handles.water_cool,'Min');
% set(handles.water_cool,'Value',minVal);
% minVal = get(handles.air_cool,'Min');
% set(handles.air_cool,'Value',minVal);
%Heat source
handles.val.mass_oil=0;
handles.val.temperature_heat=0;
handles.val.pressure_in=0;
set(handles.massflow,'String',handles.val.mass_oil)
set(handles.temperature_heat,'String',handles.val.temperature_heat)
if (get(handles.water_heat,'Value')==get(handles.water_heat,'Max'))
set(handles.pressure_in,'String',handles.val.pressure_in)
end
%Cycle properties
handles.val.start_pressure=0;
handles.val.steps=0;
handles.val.end_pressure=0;
handles.val.overheat=0;
set(handles.start_pressure,'String',handles.val.start_pressure)
set(handles.steps,'String',handles.val.steps)
set(handles.end_pressure,'String',handles.val.end_pressure)
set(handles.end_pressure,'String',handles.val.end_pressure)
set(handles.overheat,'String',handles.val.overheat)
%Component data
handles.val.effic_t=0;
handles.val.effic_p=0;
set(handles.effic_t,'String',handles.val.effic_t)
set(handles.effic_p,'String',handles.val.effic_p)
%Cooling
handles.val.temp_coolt = 0;
%Pinch-Points & Reheater efficency
handles.val.effic_reheat=0;
handles.val.pp_cond=0;
handles.val.pressure_drop=0;
handles.val.pp_preheater=0;
handles.val.temp_rise_coolt=0;
set(handles.effic_reheat,'String',handles.val.effic_reheat)
set(handles.pp_kond,'String',handles.val.pp_cond)
set(handles.pressure_drop,'String',handles.val.pressure_drop)
set(handles.pp_preheater,'String',handles.val.pp_preheater)
set(handles.temp_rise_coolt,'String',handles.val.temp_rise_coolt)
97
if (get(handles.default_val,'Value')==get(handles.default_val,'Max'))
set(handles.effic_reheat,'Style','edit')
set(handles.pp_kond,'Style','edit')
set(handles.pressure_drop,'Style','edit')
set(handles.pp_preheater,'Style','edit')
set(handles.temp_rise_coolt,'Style','edit')
set(findobj(handles.uipanel21,'style','edit'),'Backgroundcolor','white')
end
%Nollställ grafer och resultat
cla(handles.T_s);
cla(handles.T_Q);
set(handles.effic,'String','-');
set(handles.substance,'String','-');
set(handles.cycle,'String','-');
set(handles.mass_fluid,'String','-');
set(handles.power,'String','-');
set(handles.pressure,'String','-');
set(handles.tout_heat,'String','-');
set(handles.cool_out,'String','-');
set(handles.uipanel13,'BackgroundColor',[0.94,0.94,0.94])
set(handles.uipanel18,'BackgroundColor',[0.94,0.94,0.94])
set(handles.pp_new_descrip,'Visible','off');
set(handles.pp_new,'Visible','off');
set(handles.pp_new_unit,'Visible','off');
set(handles.text88,'Visible','off');
set(handles.temp_coolt,'Visible','off');
set(findobj(handles.figure1,'style','edit'),'string','0');%Nollställ alla
edit objekt.
set(findobj(handles.figure1,'style','checkbox'),'Value',0)
% --- Executes on button press in select.
%select substance
function select_Callback(hObject, eventdata, handles)
% hObject
handle to select (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
set(findobj(handles.uipanel13,'style','checkbox'),'Value',1)
% --- Executes on button press in remove.
%Deselect substance
function remove_Callback(hObject, eventdata, handles)
% hObject
handle to remove (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
set(findobj(handles.uipanel13,'style','checkbox'),'Value',0)
% --- Executes on button press in search_power.
function search_power_Callback(hObject, eventdata, handles)
98
% hObject
handle to search_power (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
if (get(hObject,'Value')==get(hObject,'Max'))
minVal = get(handles.search_effic,'Min');
set(handles.search_effic,'Value',minVal);
end
% Hint: get(hObject,'Value') returns toggle state of search_power
% --- Executes on button press in search_effic.
function search_effic_Callback(hObject, eventdata, handles)
% hObject
handle to search_effic (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
if (get(hObject,'Value')==get(hObject,'Max'))
minVal = get(handles.search_power,'Min');
set(handles.search_power,'Value',minVal);
end
% Hint: get(hObject,'Value') returns toggle state of search_effic
function effic_reheat_Callback(hObject, eventdata, handles)
% hObject
handle to effic_reheat (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of effic_reheat as text
%
str2double(get(hObject,'String')) returns contents of effic_reheat
as a double
effic_reheat = str2double(get(hObject,'String'));
% if isnan(effic_reheat)
%
set(hObject, 'String', 0);
%
errordlg('Input must be a number','Error','on');
% end
handles.val.effic_reheat=effic_reheat;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function effic_reheat_CreateFcn(hObject, eventdata, handles)
% hObject
handle to effic_reheat (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
function pp_kond_Callback(hObject, eventdata, handles)
% hObject
handle to pp_kond (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
99
% Hints: get(hObject,'String') returns contents of pp_kond as text
%
str2double(get(hObject,'String')) returns contents of pp_kond as a
double
pp_cond = str2double(get(hObject,'String'));
% if isnan(pp_kond)
%
set(hObject, 'String', 0);
%
errordlg('Input must be a number','Error','on');
% end
handles.val.pp_cond=pp_cond;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function pp_kond_CreateFcn(hObject, eventdata, handles)
% hObject
handle to pp_kond (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
function pressure_drop_Callback(hObject, eventdata, handles)
% hObject
handle to pressure_drop (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of pressure_drop as text
%
str2double(get(hObject,'String')) returns contents of
pressure_drop as a double
pressure_drop = str2double(get(hObject,'String'));
% if isnan(pressure_drop)
%
set(hObject, 'String', 0);
%
errordlg('Input must be a number','Error','on');
% end
handles.val.pressure_drop=pressure_drop;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function pressure_drop_CreateFcn(hObject, eventdata, handles)
% hObject
handle to pressure_drop (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
function pp_preheater_Callback(hObject, eventdata, handles)
% hObject
handle to pp_preheater (see GCBO)
100
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
pp_preheater =str2double(get(hObject,'String'));
% if isnan(pp_preheater)
%
set(hObject, 'String', 0);
%
errordlg('Input must be a number','Error','on');
% end
handles.val.pp_preheater = pp_preheater;
guidata(hObject,handles)
% Hints: get(hObject,'String') returns contents of pp_preheater as text
%
str2double(get(hObject,'String')) returns contents of pp_preheater
as a double
% --- Executes during object creation, after setting all properties.
function pp_preheater_CreateFcn(hObject, eventdata, handles)
% hObject
handle to pp_preheater (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
% --- Executes on button press in default_val.
function default_val_Callback(hObject, eventdata, handles)
% hObject
handle to default_val (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hint: get(hObject,'Value') returns toggle state of default_val
if (get(handles.default_val,'Value')==get(handles.default_val,'Max'))
set(handles.effic_reheat,'Style','text')
set(handles.effic_reheat,'String','80')
set(handles.pp_kond,'Style','text')
set(handles.pp_kond,'String','2')
set(handles.pressure_drop,'Style','text')
set(handles.pressure_drop,'String','5')
set(handles.pp_preheater,'Style','text')
set(handles.pp_preheater,'String','10')
set(handles.temp_rise_coolt,'Style','text')
set(handles.temp_rise_coolt,'String','10')
set(findobj(handles.uipanel21,'style','text'),'BackgroundColor',[0.94,0.94,
0.94])
end
if (get(handles.default_val,'Value')==get(handles.default_val,'Min'))
set(handles.effic_reheat,'Style','edit')
set(handles.effic_reheat,'String','0')
set(handles.pp_kond,'Style','edit')
set(handles.pp_kond,'String','0')
set(handles.pressure_drop,'Style','edit')
set(handles.pressure_drop,'String','0')
set(handles.pp_preheater,'Style','edit')
set(handles.pp_preheater,'String','0')
set(handles.temp_rise_coolt,'Style','edit')
101
set(handles.temp_rise_coolt,'String','0')
set(findobj(handles.uipanel21,'style','edit'),'BackgroundColor','white')
end
function temp_rise_coolt_Callback(hObject, eventdata, handles)
% hObject
handle to temp_rise_coolt (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of temp_rise_coolt as text
%
str2double(get(hObject,'String')) returns contents of
temp_rise_coolt as a double
temp_rise_coolt = str2double(get(hObject,'String'));
handles.val.temp_rise_coolt = temp_rise_coolt;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function temp_rise_coolt_CreateFcn(hObject, eventdata, handles)
% hObject
handle to temp_rise_coolt (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
% --- Executes on button press in default_temp_in.
function default_temp_in_Callback(hObject, eventdata, handles)
% hObject
handle to default_temp_in (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hint: get(hObject,'Value') returns toggle state of default_temp_in
if
(get(handles.default_temp_in,'Value')==get(handles.default_temp_in,'Max'))
set(handles.temp_coolt,'Style','text')
if (get(handles.water_cool,'Value')==get(handles.water_cool,'Max'))
set(handles.temp_coolt,'String','10')
set(handles.temp_coolt,'BackgroundColor',[0.94 0.94 0.94])
end
if (get(handles.air_cool,'Value')==get(handles.air_cool,'Max'))
set(handles.temp_coolt,'String','25')
set(handles.temp_coolt,'BackgroundColor',[0.94 0.94 0.94])
end
end
if
(get(handles.default_temp_in,'Value')==get(handles.default_temp_in,'Min'))
set(handles.temp_coolt,'style','edit')
set(handles.temp_coolt,'String','0')
set(handles.temp_coolt,'BackgroundColor','white')
end
102
function temp_coolt_Callback(hObject, eventdata, handles)
% hObject
handle to temp_coolt (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of temp_coolt as text
%
str2double(get(hObject,'String')) returns contents of temp_coolt
as a double
temp_coolt = str2double(get(hObject,'String'));
handles.val.temp_coolt = temp_coolt;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function temp_coolt_CreateFcn(hObject, eventdata, handles)
% hObject
handle to temp_coolt (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
% -------------------------------------------------------------------function plot_T_Q_Callback(hObject, eventdata, handles)
% hObject
handle to plot_T_Q (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
axes2fig = figure;
axes2copy = copyobj(handles.T_Q,axes2fig);
set(axes2copy,'Units','Normalized',...
'Position',[.10,.10,.80,.80])
handles.axes2fig = axes2fig;
handles.axes2copy = axes2copy;
title('T-Q')
xlabel('Q(W)')
ylabel('T(K)')
guidata(hObject,handles);
% -------------------------------------------------------------------function plot_T_s_Callback(hObject, eventdata, handles)
% hObject
handle to plot_T_s (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Displays contents of axes1 at larger size in a new figure
axes1fig = figure;
axes1copy = copyobj(handles.T_s,axes1fig);
set(axes1copy,'Units','Normalized',...
'Position',[.10,.10,.80,.80])
handles.axes1fig = axes1fig;
handles.axes1copy = axes1copy;
title('T-s')
xlabel('s(J/kgK)')
ylabel('T(K)')
guidata(hObject,handles);
103
% -------------------------------------------------------------------function plot_axes1_Callback(hObject, eventdata, handles)
% hObject
handle to plot_axes1 (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% -------------------------------------------------------------------function plot_axes2_Callback(hObject, eventdata, handles)
% hObject
handle to plot_axes2 (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% --- Executes on button press in Turb_calc.
function Turb_calc_Callback(hObject, eventdata, handles)
% hObject
handle to Turb_calc (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
run Turbine_calc
8.2 Heat source files
%##########################################################################
%##
##
%##
Enthalpy difference Oil
##
%##
##
%##########################################################################
%
%function [ h2_h1] = h_diff( T_2,T_1 )
% Insert the two temperatures and the enthalpy difference is returned.
% T_2>T_1. Temperatures in degree Celsius
function [ h2_h1] = h_diff( T_2,T_1 )
%Enthalpy differnce as a function of temperature
A = 0.415;
B = 0.0009;
density_oil = 870*10^-3;
T2 = T_2;
T1 = T_1;
h2_h1 = ((A/sqrt(density_oil))*(T2-T1)+B*((T2^2-T1^2)/2+15*(T1-T2)))*4186;
end
%##########################################################################
%##
##
%##
Temperature iteration oil
##
%##
##
%##########################################################################
%
%function [ T1] = oil_source( T_kand,q )
%Input known temperature in degree Celsius and the known transfered
%specific heat.
104
function [ T1] = oil_source( T_kand,q )
A = 0.415;
B = 0.0009;
density_oil = 870*10^-3;
T2 = T_kand;
RLX = 0.8;
T1 = T2;
err = 20;
err_der=1000;
rak=0;
qoil = q;
qtest = 1000000;
while abs(err)>1
T1 = T1-RLX*(err/err_der);
qtest = ((A/sqrt(density_oil))*(T2-T1)+B*((T2^2-T1^2)/2+15*(T1T2)))*4186;
Cp = (A/sqrt(density_oil)+B*(T1-15))*4186;
err = qoil-qtest;
err_der = Cp;
rak = rak+1;
end
end
%##########################################################################
%##
##
%##
Temperature iteration water
##
%##
##
%##########################################################################
%
%function [ T1 ] = water_source( T_kand,q,P_water )
%Input known temperature in degree Kelvin,the known transfered
%specific heat in J/kg and the pressure in kPa.
function [ T1 ] = water_source( T_kand,q,P_water )
T2 = T_kand;
P = P_water;
q_kand = q;
RLX = 0.8;
T1 = T2;
err = 20;
err_der = 1000;
while abs(err)>1
T1 = T1-RLX*(err/err_der);
qtest =refpropm('H','T',T2,'P',P,'water')refpropm('H','T',T1,'P',P,'water');
err = q_kand-qtest;
err_der = (refpropm('C','T',T1,'P',P,'water'));
end
end
105
9 Appendix B
9.1 Turbine
%##########################################################################
%##
##
%##
Turbine GUI
##
%##
Mikael Olsson
##
%##
##
%##########################################################################
function varargout = Turbine_calc(varargin)
% TURBINE_CALC M-file for Turbine_calc.fig
%
TURBINE_CALC, by itself, creates a new TURBINE_CALC or raises the
existing
%
singleton*.
%
%
H = TURBINE_CALC returns the handle to a new TURBINE_CALC or the
handle to
%
the existing singleton*.
%
%
TURBINE_CALC('CALLBACK',hObject,eventData,handles,...) calls the
local
%
function named CALLBACK in TURBINE_CALC.M with the given input
arguments.
%
%
TURBINE_CALC('Property','Value',...) creates a new TURBINE_CALC or
raises the
%
existing singleton*. Starting from the left, property value pairs
are
%
applied to the GUI before Turbine_calc_OpeningFcn gets called. An
%
unrecognized property name or invalid value makes property
application
%
stop. All inputs are passed to Turbine_calc_OpeningFcn via
varargin.
%
%
*See GUI Options on GUIDE's Tools menu. Choose "GUI allows only one
%
instance to run (singleton)".
%
% See also: GUIDE, GUIDATA, GUIHANDLES
% Edit the above text to modify the response to help Turbine_calc
% Last Modified by GUIDE v2.5 09-Jul-2012 10:09:42
% Begin initialization code - DO NOT EDIT
gui_Singleton = 1;
gui_State = struct('gui_Name',
mfilename, ...
'gui_Singleton', gui_Singleton, ...
'gui_OpeningFcn', @Turbine_calc_OpeningFcn, ...
'gui_OutputFcn', @Turbine_calc_OutputFcn, ...
'gui_LayoutFcn', [] , ...
'gui_Callback',
[]);
if nargin && ischar(varargin{1})
gui_State.gui_Callback = str2func(varargin{1});
end
if nargout
[varargout{1:nargout}] = gui_mainfcn(gui_State, varargin{:});
106
else
gui_mainfcn(gui_State, varargin{:});
end
% End initialization code - DO NOT EDIT
% --- Executes just before Turbine_calc is made visible.
function Turbine_calc_OpeningFcn(hObject, eventdata, handles, varargin)
% This function has no output args, see OutputFcn.
% hObject
handle to figure
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% varargin
command line arguments to Turbine_calc (see VARARGIN)
% Choose default command line output for Turbine_calc
handles.output = hObject;
global EXPORT_VALUES
set(handles.h04,'String',EXPORT_VALUES(1)/10^3);
set(handles.P04,'String',EXPORT_VALUES(4)/10^2);
set(handles.s04,'String',EXPORT_VALUES(2)/10^3);
set(handles.T04,'String',EXPORT_VALUES(3));
set(handles.P05,'String',EXPORT_VALUES(9)/10^2);
set(handles.s05,'String',EXPORT_VALUES(7)/10^3);
set(handles.mass,'String',EXPORT_VALUES(10));
set(handles.text337,'string',EXPORT_VALUES(11));
set(handles.text334,'string',EXPORT_VALUES(12));
Vratio = EXPORT_VALUES(12)/EXPORT_VALUES(11)
set(handles.text340,'string',Vratio);
set(handles.Angles,'visible','off');
set(handles.uipanel12,'visible','on')
set(handles.Rad_Ma,'visible','off')
bild = imread('stagen.bmp');
axes(handles.stage_pic)
imshow(bild);
axis off
% Update handles structure
guidata(hObject, handles);
% UIWAIT makes Turbine_calc wait for user response (see UIRESUME)
% uiwait(handles.figure1);
% --- Outputs from this function are returned to the command line.
function varargout = Turbine_calc_OutputFcn(hObject, eventdata, handles)
% varargout cell array for returning output args (see VARARGOUT);
% hObject
handle to figure
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Get default command line output from handles structure
varargout{1} = handles.output;
function rpm_Callback(hObject, eventdata, handles)
% hObject
handle to rpm (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
107
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of rpm as text
%
str2double(get(hObject,'String')) returns contents of rpm as a
double
rpm = str2double(get(hObject,'String'));
% if ~isnan(rpm) && ~isnan(handles.radius)
%
omega = (rpm/60)*2*pi;
%
U_m = omega*radius;
%
set(handles.text58,'String',U_m);
% end
handles.val.rpm = rpm;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function rpm_CreateFcn(hObject, eventdata, handles)
% hObject
handle to rpm (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
function radius_Callback(hObject, eventdata, handles)
% hObject
handle to radius (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of radius as text
%
str2double(get(hObject,'String')) returns contents of radius as a
double
radius = str2double(get(hObject,'String'));
% if ~isnan(handles.rpm) && ~isnan(radius)
%
omega = (handles.val.rot_speed/60)*2*pi;
%
U_m = omega*radius;
%
set(handles.text58,'String',U_m);
% end
handles.val.radius = radius;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function radius_CreateFcn(hObject, eventdata, handles)
% hObject
handle to radius (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
108
function psi_Callback(hObject, eventdata, handles)
% hObject
handle to psi (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of psi as text
%
str2double(get(hObject,'String')) returns contents of psi as a
double
psi = str2double(get(hObject,'String'));
handles.val.psi = psi;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function psi_CreateFcn(hObject, eventdata, handles)
% hObject
handle to psi (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
function phi_Callback(hObject, eventdata, handles)
% hObject
handle to phi (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of phi as text
%
str2double(get(hObject,'String')) returns contents of phi as a
double
phi = str2double(get(hObject,'String'));
handles.val.phi = phi;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function phi_CreateFcn(hObject, eventdata, handles)
% hObject
handle to phi (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
function reaction_Callback(hObject, eventdata, handles)
109
% hObject
% eventdata
% handles
handle to reaction (see GCBO)
reserved - to be defined in a future version of MATLAB
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of reaction as text
%
str2double(get(hObject,'String')) returns contents of reaction as
a double
reaction = str2double(get(hObject,'String'));
handles.val.reaction = reaction;
guidata(hObject,handles)
% --- Executes during object creation, after setting all properties.
function reaction_CreateFcn(hObject, eventdata, handles)
% hObject
handle to reaction (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
function edit8_Callback(hObject, eventdata, handles)
% hObject
handle to edit8 (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of edit8 as text
%
str2double(get(hObject,'String')) returns contents of edit8 as a
double
% --- Executes during object creation, after setting all properties.
function edit8_CreateFcn(hObject, eventdata, handles)
% hObject
handle to edit8 (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
function edit9_Callback(hObject, eventdata, handles)
% hObject
handle to edit9 (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of edit9 as text
%
str2double(get(hObject,'String')) returns contents of edit9 as a
double
110
% --- Executes during object creation, after setting all properties.
function edit9_CreateFcn(hObject, eventdata, handles)
% hObject
handle to edit9 (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
function edit10_Callback(hObject, eventdata, handles)
% hObject
handle to edit10 (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
% Hints: get(hObject,'String') returns contents of edit10 as text
%
str2double(get(hObject,'String')) returns contents of edit10 as a
double
% --- Executes during object creation, after setting all properties.
function edit10_CreateFcn(hObject, eventdata, handles)
% hObject
handle to edit10 (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
empty - handles not created until after all CreateFcns called
% Hint: edit controls usually have a white background on Windows.
%
See ISPC and COMPUTER.
if ispc && isequal(get(hObject,'BackgroundColor'),
get(0,'defaultUicontrolBackgroundColor'))
set(hObject,'BackgroundColor','white');
end
% --- Executes on button press in calc.
function calc_Callback(hObject, eventdata, handles)
% hObject
handle to calc (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
cla(handles.veltri_st1);
cla(handles.veltri_last);
set(findobj(handles.Rad_Ma,'style','text'),'string','0');
set(handles.text60,'string','Height 1')
set(handles.text136,'string','Height 2')
set(handles.text147,'string','Height 3')
set(handles.text147,'string','Height 3')
set(handles.text158,'string','Mach 1')
111
set(handles.text169,'string','Mach 2')
set(handles.text180,'string','Mach 3')
set(handles.text311,'string','Mach 2 rel')
set(handles.text322,'string','Mach 3 rel')
set(handles.text107,'string','Stage 1')
set(handles.text111,'string','Stage 2')
set(handles.text112,'string','Stage 3')
set(handles.text113,'string','Stage 4')
set(handles.text114,'string','Stage 5')
set(handles.text115,'string','Stage 6')
set(handles.text116,'string','Stage 7')
set(handles.text117,'string','Stage 8')
set(handles.text118,'string','Stage 9')
set(handles.text119,'string','Stage 10')
n_stage=0;
Psi=0;
Reac_vek=0;
Cx1=0;
C1=0;
C2=0;
C3=0;
W2=0;
W3=0;
alfa2=0;
M1=0;
alfa3=0;
M2=0;
beta2=0;
M3=0;
beta3=0;
M3_rel=0;
station1_height=0;
str_height=0;
rot_height=0;
s1_def = 0;
h01_def = 0;
P01_def = 0;
T01_def = 0;
P0kond_def = 0;
T0kond_def = 0;
s0kond_def = 0;
global EXPORT_VALUES
global fluid_select
N = handles.val.rpm;
r_m = handles.val.radius;
omega = (N/60)*2*pi;
U_m = r_m*omega;
mass = EXPORT_VALUES(10);
Reac_def = handles.val.reaction;
Psi_def = handles.val.psi;
Phi_def = handles.val.phi;
s1_def = EXPORT_VALUES(2);
h01_def = EXPORT_VALUES(1);
P01_def = EXPORT_VALUES(4);
T01_def = EXPORT_VALUES(3);
P0kond_def = EXPORT_VALUES(9);
T0kond_def = EXPORT_VALUES(5);
s0kond_def = EXPORT_VALUES(7);
amne = fluid_select;
[n_stage W_turb effic Psi Reac_vek Cx1 C1 C2 C3 W2 W3 M1 M2 M2_rel M3
M3_rel station1_height str_height rot_height alfa2 alfa3 beta2 beta3]=...
Turbine(Psi_def,Phi_def,Reac_def,N,U_m,r_m,mass,s1_def,h01_def,T01_def,P01_
def,P0kond_def,T0kond_def,s0kond_def,amne);
set(handles.text99,'string',round(100*Psi(n_stage))/100);
set(handles.text102,'string',round(100*Reac_vek(n_stage))/100);
%%Performance
112
set(handles.text302,'string',n_stage);
set(handles.text306,'string',W_turb);
set(handles.text308,'string',effic);
%%Flow Angles
set(handles.text268,'string',round(100*alfa2(1))/100);
set(handles.text272,'string',round(100*alfa2(n_stage))/100);
set(handles.text271,'string',round(100*alfa3(1))/100);
set(handles.text273,'string',round(100*alfa3(n_stage))/100);
set(handles.text275,'string',round(100*beta2(1))/100);
set(handles.text276,'string',round(100*beta2(n_stage))/100);
set(handles.text278,'string',round(100*beta3(1))/100);
set(handles.text279,'string',round(100*beta3(n_stage))/100);
%%RAD_MA
if n_stage==1
set(handles.R11,'String',round(10^4*station1_height(1))/10^4);
set(handles.R21,'String',round(10^4*str_height(1))/10^4);
set(handles.R31,'String',round(10^4*rot_height(1))/10^4);
set(handles.Ma11,'String',round(10^2*M1(1))/10^2);
set(handles.Ma21,'String',round(10^2*M2(1))/10^2);
set(handles.Ma31,'String',round(10^2*M3(1))/10^2);
set(handles.text312,'String',round(10^2*M2_rel(1))/10^2);
set(handles.text323,'String',round(10^2*M3_rel(1))/10^2);
end
if n_stage==2
set(handles.R11,'String',round(10^4*station1_height(1))/10^4);
set(handles.R12,'String',round(10^4*station1_height(2))/10^4);
set(handles.R21,'String',round(10^4*str_height(1))/10^4);
set(handles.R22,'String',round(10^4*str_height(2))/10^4);
set(handles.R31,'String',round(10^4*rot_height(1))/10^4);
set(handles.R32,'String',round(10^4*rot_height(2))/10^4);
set(handles.Ma11,'String',round(10^2*M1(1))/10^2);
set(handles.Ma12,'String',round(10^2*M1(2))/10^2);
set(handles.Ma21,'String',round(10^2*M2(1))/10^2);
set(handles.Ma22,'String',round(10^2*M2(2))/10^2);
set(handles.Ma31,'String',round(10^2*M3(1))/10^2);
set(handles.Ma32,'String',round(10^2*M3(2))/10^2);
set(handles.text312,'String',round(10^2*M2_rel(1))/10^2);
set(handles.text313,'String',round(10^2*M2_rel(2))/10^2);
set(handles.text323,'String',round(10^2*M3_rel(1))/10^2);
set(handles.text324,'String',round(10^2*M3_rel(2))/10^2);
end
if n_stage==3
set(handles.R11,'String',round(10^4*station1_height(1))/10^4);
set(handles.R12,'String',round(10^4*station1_height(2))/10^4);
set(handles.R13,'String',round(10^4*station1_height(3))/10^4);
set(handles.R21,'String',round(10^4*str_height(1))/10^4);
set(handles.R22,'String',round(10^4*str_height(2))/10^4);
set(handles.R23,'String',round(10^4*str_height(3))/10^4);
set(handles.R31,'String',round(10^4*rot_height(1))/10^4);
set(handles.R32,'String',round(10^4*rot_height(2))/10^4);
set(handles.R33,'String',round(10^4*rot_height(3))/10^4);
113
set(handles.Ma11,'String',round(10^2*M1(1))/10^2);
set(handles.Ma12,'String',round(10^2*M1(2))/10^2);
set(handles.Ma13,'String',round(10^2*M1(3))/10^2);
set(handles.Ma21,'String',round(10^2*M2(1))/10^2);
set(handles.Ma22,'String',round(10^2*M2(2))/10^2);
set(handles.Ma23,'String',round(10^2*M2(3))/10^2);
set(handles.Ma31,'String',round(10^2*M3(1))/10^2);
set(handles.Ma32,'String',round(10^2*M3(2))/10^2);
set(handles.Ma33,'String',round(10^2*M3(3))/10^2);
set(handles.text312,'String',round(10^2*M2_rel(1))/10^2);
set(handles.text313,'String',round(10^2*M2_rel(2))/10^2);
set(handles.text314,'String',round(10^2*M2_rel(3))/10^2);
set(handles.text323,'String',round(10^2*M3_rel(1))/10^2);
set(handles.text324,'String',round(10^2*M3_rel(2))/10^2);
set(handles.text325,'String',round(10^2*M3_rel(3))/10^2);
end
if n_stage==4
set(handles.R11,'String',round(10^4*station1_height(1))/10^4);
set(handles.R12,'String',round(10^4*station1_height(2))/10^4);
set(handles.R13,'String',round(10^4*station1_height(3))/10^4);
set(handles.R14,'String',round(10^4*station1_height(4))/10^4);
set(handles.R21,'String',round(10^4*str_height(1))/10^4);
set(handles.R22,'String',round(10^4*str_height(2))/10^4);
set(handles.R23,'String',round(10^4*str_height(3))/10^4);
set(handles.R24,'String',round(10^4*str_height(4))/10^4);
set(handles.R31,'String',round(10^4*rot_height(1))/10^4);
set(handles.R32,'String',round(10^4*rot_height(2))/10^4);
set(handles.R33,'String',round(10^4*rot_height(3))/10^4);
set(handles.R34,'String',round(10^4*rot_height(4))/10^4);
set(handles.Ma11,'String',round(10^2*M1(1))/10^2);
set(handles.Ma12,'String',round(10^2*M1(2))/10^2);
set(handles.Ma13,'String',round(10^2*M1(3))/10^2);
set(handles.Ma14,'String',round(10^2*M1(4))/10^2);
set(handles.Ma21,'String',round(10^2*M2(1))/10^2);
set(handles.Ma22,'String',round(10^2*M2(2))/10^2);
set(handles.Ma23,'String',round(10^2*M2(3))/10^2);
set(handles.Ma24,'String',round(10^2*M2(4))/10^2);
set(handles.Ma31,'String',round(10^2*M3(1))/10^2);
set(handles.Ma32,'String',round(10^2*M3(2))/10^2);
set(handles.Ma33,'String',round(10^2*M3(3))/10^2);
set(handles.Ma34,'String',round(10^2*M3(4))/10^2);
set(handles.text312,'String',round(10^2*M2_rel(1))/10^2);
set(handles.text313,'String',round(10^2*M2_rel(2))/10^2);
set(handles.text314,'String',round(10^2*M2_rel(3))/10^2);
set(handles.text315,'String',round(10^2*M2_rel(4))/10^2);
set(handles.text323,'String',round(10^2*M3_rel(1))/10^2);
set(handles.text324,'String',round(10^2*M3_rel(2))/10^2);
set(handles.text325,'String',round(10^2*M3_rel(3))/10^2);
set(handles.text326,'String',round(10^2*M3_rel(4))/10^2);
end
if n_stage==5
set(handles.R11,'String',round(10^4*station1_height(1))/10^4);
set(handles.R12,'String',round(10^4*station1_height(2))/10^4);
set(handles.R13,'String',round(10^4*station1_height(3))/10^4);
set(handles.R14,'String',round(10^4*station1_height(4))/10^4);
set(handles.R15,'String',round(10^4*station1_height(5))/10^4);
set(handles.R21,'String',round(10^4*str_height(1))/10^4);
set(handles.R22,'String',round(10^4*str_height(2))/10^4);
114
set(handles.R23,'String',round(10^4*str_height(3))/10^4);
set(handles.R24,'String',round(10^4*str_height(4))/10^4);
set(handles.R25,'String',round(10^4*str_height(5))/10^4);
set(handles.R31,'String',round(10^4*rot_height(1))/10^4);
set(handles.R32,'String',round(10^4*rot_height(2))/10^4);
set(handles.R33,'String',round(10^4*rot_height(3))/10^4);
set(handles.R34,'String',round(10^4*rot_height(4))/10^4);
set(handles.R35,'String',round(10^4*rot_height(5))/10^4);
set(handles.Ma11,'String',round(10^2*M1(1))/10^2);
set(handles.Ma12,'String',round(10^2*M1(2))/10^2);
set(handles.Ma13,'String',round(10^2*M1(3))/10^2);
set(handles.Ma14,'String',round(10^2*M1(4))/10^2);
set(handles.Ma15,'String',round(10^2*M1(5))/10^2);
set(handles.Ma21,'String',round(10^2*M2(1))/10^2);
set(handles.Ma22,'String',round(10^2*M2(2))/10^2);
set(handles.Ma23,'String',round(10^2*M2(3))/10^2);
set(handles.Ma24,'String',round(10^2*M2(4))/10^2);
set(handles.Ma25,'String',round(10^2*M2(5))/10^2);
set(handles.Ma31,'String',round(10^2*M3(1))/10^2);
set(handles.Ma32,'String',round(10^2*M3(2))/10^2);
set(handles.Ma33,'String',round(10^2*M3(3))/10^2);
set(handles.Ma34,'String',round(10^2*M3(4))/10^2);
set(handles.Ma35,'String',round(10^2*M3(5))/10^2);
set(handles.text312,'String',round(10^2*M2_rel(1))/10^2);
set(handles.text313,'String',round(10^2*M2_rel(2))/10^2);
set(handles.text314,'String',round(10^2*M2_rel(3))/10^2);
set(handles.text315,'String',round(10^2*M2_rel(4))/10^2);
set(handles.text316,'String',round(10^2*M2_rel(5))/10^2);
set(handles.text323,'String',round(10^2*M3_rel(1))/10^2);
set(handles.text324,'String',round(10^2*M3_rel(2))/10^2);
set(handles.text325,'String',round(10^2*M3_rel(3))/10^2);
set(handles.text326,'String',round(10^2*M3_rel(4))/10^2);
set(handles.text327,'String',round(10^2*M3_rel(5))/10^2);
end
if n_stage==6
set(handles.R11,'String',round(10^4*station1_height(1))/10^4);
set(handles.R12,'String',round(10^4*station1_height(2))/10^4);
set(handles.R13,'String',round(10^4*station1_height(3))/10^4);
set(handles.R14,'String',round(10^4*station1_height(4))/10^4);
set(handles.R15,'String',round(10^4*station1_height(5))/10^4);
set(handles.R16,'String',round(10^4*station1_height(6))/10^4);
set(handles.R21,'String',round(10^4*str_height(1))/10^4);
set(handles.R22,'String',round(10^4*str_height(2))/10^4);
set(handles.R23,'String',round(10^4*str_height(3))/10^4);
set(handles.R24,'String',round(10^4*str_height(4))/10^4);
set(handles.R25,'String',round(10^4*str_height(5))/10^4);
set(handles.R26,'String',round(10^4*str_height(6))/10^4);
set(handles.R31,'String',round(10^4*rot_height(1))/10^4);
set(handles.R32,'String',round(10^4*rot_height(2))/10^4);
set(handles.R33,'String',round(10^4*rot_height(3))/10^4);
set(handles.R34,'String',round(10^4*rot_height(4))/10^4);
set(handles.R35,'String',round(10^4*rot_height(5))/10^4);
set(handles.R36,'String',round(10^4*rot_height(6))/10^4);
set(handles.Ma11,'String',round(10^2*M1(1))/10^2);
set(handles.Ma12,'String',round(10^2*M1(2))/10^2);
set(handles.Ma13,'String',round(10^2*M1(3))/10^2);
set(handles.Ma14,'String',round(10^2*M1(4))/10^2);
set(handles.Ma15,'String',round(10^2*M1(5))/10^2);
115
set(handles.Ma16,'String',round(10^2*M1(6))/10^2);
set(handles.Ma21,'String',round(10^2*M2(1))/10^2);
set(handles.Ma22,'String',round(10^2*M2(2))/10^2);
set(handles.Ma23,'String',round(10^2*M2(3))/10^2);
set(handles.Ma24,'String',round(10^2*M2(4))/10^2);
set(handles.Ma25,'String',round(10^2*M2(5))/10^2);
set(handles.Ma26,'String',round(10^2*M2(6))/10^2);
set(handles.Ma31,'String',round(10^2*M3(1))/10^2);
set(handles.Ma32,'String',round(10^2*M3(2))/10^2);
set(handles.Ma33,'String',round(10^2*M3(3))/10^2);
set(handles.Ma34,'String',round(10^2*M3(4))/10^2);
set(handles.Ma35,'String',round(10^2*M3(5))/10^2);
set(handles.Ma36,'String',round(10^2*M3(6))/10^2);
set(handles.text312,'String',round(10^2*M2_rel(1))/10^2);
set(handles.text313,'String',round(10^2*M2_rel(2))/10^2);
set(handles.text314,'String',round(10^2*M2_rel(3))/10^2);
set(handles.text315,'String',round(10^2*M2_rel(4))/10^2);
set(handles.text316,'String',round(10^2*M2_rel(5))/10^2);
set(handles.text317,'String',round(10^2*M2_rel(6))/10^2);
set(handles.text323,'String',round(10^2*M3_rel(1))/10^2);
set(handles.text324,'String',round(10^2*M3_rel(2))/10^2);
set(handles.text325,'String',round(10^2*M3_rel(3))/10^2);
set(handles.text326,'String',round(10^2*M3_rel(4))/10^2);
set(handles.text327,'String',round(10^2*M3_rel(5))/10^2);
set(handles.text328,'String',round(10^2*M3_rel(6))/10^2);
end
if n_stage==7
set(handles.R11,'String',round(10^4*station1_height(1))/10^4);
set(handles.R12,'String',round(10^4*station1_height(2))/10^4);
set(handles.R13,'String',round(10^4*station1_height(3))/10^4);
set(handles.R14,'String',round(10^4*station1_height(4))/10^4);
set(handles.R15,'String',round(10^4*station1_height(5))/10^4);
set(handles.R16,'String',round(10^4*station1_height(6))/10^4);
set(handles.R17,'String',round(10^4*station1_height(7))/10^4);
set(handles.R21,'String',round(10^4*str_height(1))/10^4);
set(handles.R22,'String',round(10^4*str_height(2))/10^4);
set(handles.R23,'String',round(10^4*str_height(3))/10^4);
set(handles.R24,'String',round(10^4*str_height(4))/10^4);
set(handles.R25,'String',round(10^4*str_height(5))/10^4);
set(handles.R26,'String',round(10^4*str_height(6))/10^4);
set(handles.R27,'String',round(10^4*str_height(7))/10^4);
set(handles.R31,'String',round(10^4*rot_height(1))/10^4);
set(handles.R32,'String',round(10^4*rot_height(2))/10^4);
set(handles.R33,'String',round(10^4*rot_height(3))/10^4);
set(handles.R34,'String',round(10^4*rot_height(4))/10^4);
set(handles.R35,'String',round(10^4*rot_height(5))/10^4);
set(handles.R36,'String',round(10^4*rot_height(6))/10^4);
set(handles.R37,'String',round(10^4*rot_height(7))/10^4);
set(handles.Ma11,'String',round(10^2*M1(1))/10^2);
set(handles.Ma12,'String',round(10^2*M1(2))/10^2);
set(handles.Ma13,'String',round(10^2*M1(3))/10^2);
set(handles.Ma14,'String',round(10^2*M1(4))/10^2);
set(handles.Ma15,'String',round(10^2*M1(5))/10^2);
set(handles.Ma16,'String',round(10^2*M1(6))/10^2);
set(handles.Ma17,'String',round(10^2*M1(7))/10^2);
set(handles.Ma21,'String',round(10^2*M2(1))/10^2);
set(handles.Ma22,'String',round(10^2*M2(2))/10^2);
set(handles.Ma23,'String',round(10^2*M2(3))/10^2);
set(handles.Ma24,'String',round(10^2*M2(4))/10^2);
116
set(handles.Ma25,'String',round(10^2*M2(5))/10^2);
set(handles.Ma26,'String',round(10^2*M2(6))/10^2);
set(handles.Ma27,'String',round(10^2*M2(7))/10^2);
set(handles.Ma31,'String',round(10^2*M3(1))/10^2);
set(handles.Ma32,'String',round(10^2*M3(2))/10^2);
set(handles.Ma33,'String',round(10^2*M3(3))/10^2);
set(handles.Ma34,'String',round(10^2*M3(4))/10^2);
set(handles.Ma35,'String',round(10^2*M3(5))/10^2);
set(handles.Ma36,'String',round(10^2*M3(6))/10^2);
set(handles.Ma37,'String',round(10^2*M3(7))/10^2);
set(handles.text312,'String',round(10^2*M2_rel(1))/10^2);
set(handles.text313,'String',round(10^2*M2_rel(2))/10^2);
set(handles.text314,'String',round(10^2*M2_rel(3))/10^2);
set(handles.text315,'String',round(10^2*M2_rel(4))/10^2);
set(handles.text316,'String',round(10^2*M2_rel(5))/10^2);
set(handles.text317,'String',round(10^2*M2_rel(6))/10^2);
set(handles.text318,'String',round(10^2*M2_rel(7))/10^2);
set(handles.text323,'String',round(10^2*M3_rel(1))/10^2);
set(handles.text324,'String',round(10^2*M3_rel(2))/10^2);
set(handles.text325,'String',round(10^2*M3_rel(3))/10^2);
set(handles.text326,'String',round(10^2*M3_rel(4))/10^2);
set(handles.text327,'String',round(10^2*M3_rel(5))/10^2);
set(handles.text328,'String',round(10^2*M3_rel(6))/10^2);
set(handles.text329,'String',round(10^2*M3_rel(7))/10^2);
end
if n_stage==8
set(handles.R11,'String',round(10^4*station1_height(1))/10^4);
set(handles.R12,'String',round(10^4*station1_height(2))/10^4);
set(handles.R13,'String',round(10^4*station1_height(3))/10^4);
set(handles.R14,'String',round(10^4*station1_height(4))/10^4);
set(handles.R15,'String',round(10^4*station1_height(5))/10^4);
set(handles.R16,'String',round(10^4*station1_height(6))/10^4);
set(handles.R17,'String',round(10^4*station1_height(7))/10^4);
set(handles.R18,'String',round(10^4*station1_height(8))/10^4);
set(handles.R21,'String',round(10^4*str_height(1))/10^4);
set(handles.R22,'String',round(10^4*str_height(2))/10^4);
set(handles.R23,'String',round(10^4*str_height(3))/10^4);
set(handles.R24,'String',round(10^4*str_height(4))/10^4);
set(handles.R25,'String',round(10^4*str_height(5))/10^4);
set(handles.R26,'String',round(10^4*str_height(6))/10^4);
set(handles.R27,'String',round(10^4*str_height(7))/10^4);
set(handles.R28,'String',round(10^4*str_height(8))/10^4);
set(handles.R31,'String',round(10^4*rot_height(1))/10^4);
set(handles.R32,'String',round(10^4*rot_height(2))/10^4);
set(handles.R33,'String',round(10^4*rot_height(3))/10^4);
set(handles.R34,'String',round(10^4*rot_height(4))/10^4);
set(handles.R35,'String',round(10^4*rot_height(5))/10^4);
set(handles.R36,'String',round(10^4*rot_height(6))/10^4);
set(handles.R37,'String',round(10^4*rot_height(7))/10^4);
set(handles.R38,'String',round(10^4*rot_height(8))/10^4);
set(handles.Ma11,'String',round(10^2*M1(1))/10^2);
set(handles.Ma12,'String',round(10^2*M1(2))/10^2);
set(handles.Ma13,'String',round(10^2*M1(3))/10^2);
set(handles.Ma14,'String',round(10^2*M1(4))/10^2);
set(handles.Ma15,'String',round(10^2*M1(5))/10^2);
set(handles.Ma16,'String',round(10^2*M1(6))/10^2);
set(handles.Ma17,'String',round(10^2*M1(7))/10^2);
set(handles.Ma18,'String',round(10^2*M1(8))/10^2);
set(handles.Ma21,'String',round(10^2*M2(1))/10^2);
117
set(handles.Ma22,'String',round(10^2*M2(2))/10^2);
set(handles.Ma23,'String',round(10^2*M2(3))/10^2);
set(handles.Ma24,'String',round(10^2*M2(4))/10^2);
set(handles.Ma25,'String',round(10^2*M2(5))/10^2);
set(handles.Ma26,'String',round(10^2*M2(6))/10^2);
set(handles.Ma27,'String',round(10^2*M2(7))/10^2);
set(handles.Ma28,'String',round(10^2*M2(8))/10^2);
set(handles.Ma31,'String',round(10^2*M3(1))/10^2);
set(handles.Ma32,'String',round(10^2*M3(2))/10^2);
set(handles.Ma33,'String',round(10^2*M3(3))/10^2);
set(handles.Ma34,'String',round(10^2*M3(4))/10^2);
set(handles.Ma35,'String',round(10^2*M3(5))/10^2);
set(handles.Ma36,'String',round(10^2*M3(6))/10^2);
set(handles.Ma37,'String',round(10^2*M3(7))/10^2);
set(handles.Ma38,'String',round(10^2*M3(8))/10^2);
set(handles.text312,'String',round(10^2*M2_rel(1))/10^2);
set(handles.text313,'String',round(10^2*M2_rel(2))/10^2);
set(handles.text314,'String',round(10^2*M2_rel(3))/10^2);
set(handles.text315,'String',round(10^2*M2_rel(4))/10^2);
set(handles.text316,'String',round(10^2*M2_rel(5))/10^2);
set(handles.text317,'String',round(10^2*M2_rel(6))/10^2);
set(handles.text318,'String',round(10^2*M2_rel(7))/10^2);
set(handles.text319,'String',round(10^2*M2_rel(8))/10^2);
set(handles.text323,'String',round(10^2*M3_rel(1))/10^2);
set(handles.text324,'String',round(10^2*M3_rel(2))/10^2);
set(handles.text325,'String',round(10^2*M3_rel(3))/10^2);
set(handles.text326,'String',round(10^2*M3_rel(4))/10^2);
set(handles.text327,'String',round(10^2*M3_rel(5))/10^2);
set(handles.text328,'String',round(10^2*M3_rel(6))/10^2);
set(handles.text329,'String',round(10^2*M3_rel(7))/10^2);
set(handles.text330,'String',round(10^2*M3_rel(8))/10^2);
end
if n_stage==9
set(handles.R11,'String',round(10^4*station1_height(1))/10^4);
set(handles.R12,'String',round(10^4*station1_height(2))/10^4);
set(handles.R13,'String',round(10^4*station1_height(3))/10^4);
set(handles.R14,'String',round(10^4*station1_height(4))/10^4);
set(handles.R15,'String',round(10^4*station1_height(5))/10^4);
set(handles.R16,'String',round(10^4*station1_height(6))/10^4);
set(handles.R17,'String',round(10^4*station1_height(7))/10^4);
set(handles.R18,'String',round(10^4*station1_height(8))/10^4);
set(handles.R19,'String',round(10^4*station1_height(9))/10^4);
set(handles.R21,'String',round(10^4*str_height(1))/10^4);
set(handles.R22,'String',round(10^4*str_height(2))/10^4);
set(handles.R23,'String',round(10^4*str_height(3))/10^4);
set(handles.R24,'String',round(10^4*str_height(4))/10^4);
set(handles.R25,'String',round(10^4*str_height(5))/10^4);
set(handles.R26,'String',round(10^4*str_height(6))/10^4);
set(handles.R27,'String',round(10^4*str_height(7))/10^4);
set(handles.R28,'String',round(10^4*str_height(8))/10^4);
set(handles.R29,'String',round(10^4*str_height(9))/10^4);
set(handles.R31,'String',round(10^4*rot_height(1))/10^4);
set(handles.R32,'String',round(10^4*rot_height(2))/10^4);
set(handles.R33,'String',round(10^4*rot_height(3))/10^4);
set(handles.R34,'String',round(10^4*rot_height(4))/10^4);
set(handles.R35,'String',round(10^4*rot_height(5))/10^4);
set(handles.R36,'String',round(10^4*rot_height(6))/10^4);
set(handles.R37,'String',round(10^4*rot_height(7))/10^4);
set(handles.R38,'String',round(10^4*rot_height(8))/10^4);
set(handles.R39,'String',round(10^4*rot_height(9))/10^4);
118
set(handles.Ma11,'String',round(10^2*M1(1))/10^2);
set(handles.Ma12,'String',round(10^2*M1(2))/10^2);
set(handles.Ma13,'String',round(10^2*M1(3))/10^2);
set(handles.Ma14,'String',round(10^2*M1(4))/10^2);
set(handles.Ma15,'String',round(10^2*M1(5))/10^2);
set(handles.Ma16,'String',round(10^2*M1(6))/10^2);
set(handles.Ma17,'String',round(10^2*M1(7))/10^2);
set(handles.Ma18,'String',round(10^2*M1(8))/10^2);
set(handles.Ma19,'String',round(10^2*M1(9))/10^2);
set(handles.Ma21,'String',round(10^2*M2(1))/10^2);
set(handles.Ma22,'String',round(10^2*M2(2))/10^2);
set(handles.Ma23,'String',round(10^2*M2(3))/10^2);
set(handles.Ma24,'String',round(10^2*M2(4))/10^2);
set(handles.Ma25,'String',round(10^2*M2(5))/10^2);
set(handles.Ma26,'String',round(10^2*M2(6))/10^2);
set(handles.Ma27,'String',round(10^2*M2(7))/10^2);
set(handles.Ma28,'String',round(10^2*M2(8))/10^2);
set(handles.Ma29,'String',round(10^2*M2(9))/10^2);
set(handles.Ma31,'String',round(10^2*M3(1))/10^2);
set(handles.Ma32,'String',round(10^2*M3(2))/10^2);
set(handles.Ma33,'String',round(10^2*M3(3))/10^2);
set(handles.Ma34,'String',round(10^2*M3(4))/10^2);
set(handles.Ma35,'String',round(10^2*M3(5))/10^2);
set(handles.Ma36,'String',round(10^2*M3(6))/10^2);
set(handles.Ma37,'String',round(10^2*M3(7))/10^2);
set(handles.Ma38,'String',round(10^2*M3(8))/10^2);
set(handles.Ma39,'String',round(10^2*M3(9))/10^2);
set(handles.text312,'String',round(10^2*M2_rel(1))/10^2);
set(handles.text313,'String',round(10^2*M2_rel(2))/10^2);
set(handles.text314,'String',round(10^2*M2_rel(3))/10^2);
set(handles.text315,'String',round(10^2*M2_rel(4))/10^2);
set(handles.text316,'String',round(10^2*M2_rel(5))/10^2);
set(handles.text317,'String',round(10^2*M2_rel(6))/10^2);
set(handles.text318,'String',round(10^2*M2_rel(7))/10^2);
set(handles.text319,'String',round(10^2*M2_rel(8))/10^2);
set(handles.text320,'String',round(10^2*M2_rel(9))/10^2);
set(handles.text323,'String',round(10^2*M3_rel(1))/10^2);
set(handles.text324,'String',round(10^2*M3_rel(2))/10^2);
set(handles.text325,'String',round(10^2*M3_rel(3))/10^2);
set(handles.text326,'String',round(10^2*M3_rel(4))/10^2);
set(handles.text327,'String',round(10^2*M3_rel(5))/10^2);
set(handles.text328,'String',round(10^2*M3_rel(6))/10^2);
set(handles.text329,'String',round(10^2*M3_rel(7))/10^2);
set(handles.text330,'String',round(10^2*M3_rel(8))/10^2);
set(handles.text331,'String',round(10^2*M3_rel(9))/10^2);
end
if n_stage==10
set(handles.R11,'String',round(10^4*station1_height(1))/10^4);
set(handles.R12,'String',round(10^4*station1_height(2))/10^4);
set(handles.R13,'String',round(10^4*station1_height(3))/10^4);
set(handles.R14,'String',round(10^4*station1_height(4))/10^4);
set(handles.R15,'String',round(10^4*station1_height(5))/10^4);
set(handles.R16,'String',round(10^4*station1_height(6))/10^4);
set(handles.R17,'String',round(10^4*station1_height(7))/10^4);
set(handles.R18,'String',round(10^4*station1_height(8))/10^4);
set(handles.R19,'String',round(10^4*station1_height(9))/10^4);
set(handles.R110,'String',round(10^4*station1_height(10))/10^4);
set(handles.R21,'String',round(10^4*str_height(1))/10^4);
set(handles.R22,'String',round(10^4*str_height(2))/10^4);
119
set(handles.R23,'String',round(10^4*str_height(3))/10^4);
set(handles.R24,'String',round(10^4*str_height(4))/10^4);
set(handles.R25,'String',round(10^4*str_height(5))/10^4);
set(handles.R26,'String',round(10^4*str_height(6))/10^4);
set(handles.R27,'String',round(10^4*str_height(7))/10^4);
set(handles.R28,'String',round(10^4*str_height(8))/10^4);
set(handles.R29,'String',round(10^4*str_height(9))/10^4);
set(handles.R210,'String',round(10^4*str_height(10))/10^4);
set(handles.R31,'String',round(10^4*rot_height(1))/10^4);
set(handles.R32,'String',round(10^4*rot_height(2))/10^4);
set(handles.R33,'String',round(10^4*rot_height(3))/10^4);
set(handles.R34,'String',round(10^4*rot_height(4))/10^4);
set(handles.R35,'String',round(10^4*rot_height(5))/10^4);
set(handles.R36,'String',round(10^4*rot_height(6))/10^4);
set(handles.R37,'String',round(10^4*rot_height(7))/10^4);
set(handles.R38,'String',round(10^4*rot_height(8))/10^4);
set(handles.R39,'String',round(10^4*rot_height(9))/10^4);
set(handles.R310,'String',round(10^4*rot_height(10))/10^4);
set(handles.Ma11,'String',round(10^2*M1(1))/10^2);
set(handles.Ma12,'String',round(10^2*M1(2))/10^2);
set(handles.Ma13,'String',round(10^2*M1(3))/10^2);
set(handles.Ma14,'String',round(10^2*M1(4))/10^2);
set(handles.Ma15,'String',round(10^2*M1(5))/10^2);
set(handles.Ma16,'String',round(10^2*M1(6))/10^2);
set(handles.Ma17,'String',round(10^2*M1(7))/10^2);
set(handles.Ma18,'String',round(10^2*M1(8))/10^2);
set(handles.Ma19,'String',round(10^2*M1(9))/10^2);
set(handles.Ma110,'String',round(10^2*M1(10))/10^2);
set(handles.Ma21,'String',round(10^2*M2(1))/10^2);
set(handles.Ma22,'String',round(10^2*M2(2))/10^2);
set(handles.Ma23,'String',round(10^2*M2(3))/10^2);
set(handles.Ma24,'String',round(10^2*M2(4))/10^2);
set(handles.Ma25,'String',round(10^2*M2(5))/10^2);
set(handles.Ma26,'String',round(10^2*M2(6))/10^2);
set(handles.Ma27,'String',round(10^2*M2(7))/10^2);
set(handles.Ma28,'String',round(10^2*M2(8))/10^2);
set(handles.Ma29,'String',round(10^2*M2(9))/10^2);
set(handles.Ma210,'String',round(10^2*M2(10))/10^2);
set(handles.Ma31,'String',round(10^2*M3(1))/10^2);
set(handles.Ma32,'String',round(10^2*M3(2))/10^2);
set(handles.Ma33,'String',round(10^2*M3(3))/10^2);
set(handles.Ma34,'String',round(10^2*M3(4))/10^2);
set(handles.Ma35,'String',round(10^2*M3(5))/10^2);
set(handles.Ma36,'String',round(10^2*M3(6))/10^2);
set(handles.Ma37,'String',round(10^2*M3(7))/10^2);
set(handles.Ma38,'String',round(10^2*M3(8))/10^2);
set(handles.Ma39,'String',round(10^2*M3(9))/10^2);
set(handles.Ma310,'String',round(10^2*M3(10))/10^2);
set(handles.text312,'String',round(10^2*M2_rel(1))/10^2);
set(handles.text313,'String',round(10^2*M2_rel(2))/10^2);
set(handles.text314,'String',round(10^2*M2_rel(3))/10^2);
set(handles.text315,'String',round(10^2*M2_rel(4))/10^2);
set(handles.text316,'String',round(10^2*M2_rel(5))/10^2);
set(handles.text317,'String',round(10^2*M2_rel(6))/10^2);
set(handles.text318,'String',round(10^2*M2_rel(7))/10^2);
set(handles.text319,'String',round(10^2*M2_rel(8))/10^2);
set(handles.text320,'String',round(10^2*M2_rel(9))/10^2);
set(handles.text321,'String',round(10^2*M2_rel(10))/10^2);
set(handles.text323,'String',round(10^2*M3_rel(1))/10^2);
120
set(handles.text324,'String',round(10^2*M3_rel(2))/10^2);
set(handles.text325,'String',round(10^2*M3_rel(3))/10^2);
set(handles.text326,'String',round(10^2*M3_rel(4))/10^2);
set(handles.text327,'String',round(10^2*M3_rel(5))/10^2);
set(handles.text328,'String',round(10^2*M3_rel(6))/10^2);
set(handles.text329,'String',round(10^2*M3_rel(7))/10^2);
set(handles.text330,'String',round(10^2*M3_rel(8))/10^2);
set(handles.text331,'String',round(10^2*M3_rel(9))/10^2);
set(handles.text332,'String',round(10^2*M3_rel(10))/10^2);
end
%Veltri First stage
%AXIAL hastighet
j=1;
Y1 = [0 -Cx1];
X1 = [C2(j)*sind(alfa2(j)) C2(j)*sind(alfa2(j))];
%Absolut stat2
Y2 = [0 -C2(j)*cosd(alfa2(j))];
X2 = [C2(j)*sind(alfa2(j)) 0];
%Relativ stat2
Y3 = [0 -W2(j)*cosd(beta2(j))];
X3 = [U_m+W2(j)*sind(beta2(j)) U_m];
%U_M
X4 = [U_m 0];
Y4 = [-C2(j)*cosd(alfa2(j)) -C2(j)*cosd(alfa2(j))];
%Absolut stat3
Y5 = [0 -C3(j)*cosd(alfa3(j))];
X5 = [C2(j)*sind(alfa2(j)) C2(j)*sind(alfa2(j))+C3(j)*sind(-alfa3(j))];
%Relativ stat3
Y6 = [0 -W3(j)*cosd(beta3(j))];
X6 = [C2(j)*sind(alfa2(j)) C2(j)*sind(alfa2(j))+W3(j)*sind(-beta3(j))];
%U_m
X7 = [C2(j)*sind(alfa2(j))+C3(j)*sind(-alfa3(j))
C2(j)*sind(alfa2(j))+W3(j)*sind(-beta3(j))];
Y7 = [-W3(j)*cosd(beta3(j)) -W3(j)*cosd(beta3(j))];
%Veltri last stage
j=n_stage;
Y8 = [0 -Cx1];
X8 = [C2(j)*sind(alfa2(j)) C2(j)*sind(alfa2(j))];
%Absolut stat2
Y9 = [0 -C2(j)*cosd(alfa2(j))];
X9 = [C2(j)*sind(alfa2(j)) 0];
121
%Relativ stat2
Y10 = [0 -W2(j)*cosd(beta2(j))];
X10 = [U_m+W2(j)*sind(beta2(j)) U_m];
%U_M
X11 = [U_m 0];
Y11 = [-C2(j)*cosd(alfa2(j)) -C2(j)*cosd(alfa2(j))];
%Absolut stat3
Y12 = [0 -C3(j)*cosd(alfa3(j))];
X12 = [C2(j)*sind(alfa2(j)) C2(j)*sind(alfa2(j))+C3(j)*sind(-alfa3(j))];
%Relativ stat3
Y13 = [0 -W3(j)*cosd(beta3(j))];
X13 = [C2(j)*sind(alfa2(j)) C2(j)*sind(alfa2(j))+W3(j)*sind(-beta3(j))];
%U_m
X14 = [C2(j)*sind(alfa2(j))+C3(j)*sind(-alfa3(j))
C2(j)*sind(alfa2(j))+W3(j)*sind(-beta3(j))];
Y14 = [-W3(j)*cosd(beta3(j)) -W3(j)*cosd(beta3(j))];
%plot veltri
axes(handles.veltri_st1)
title('For all but the last stage')
xlabel('m/s')
ylabel('m/s')
hold on
plot(handles.veltri_st1,X1,Y1,'g-','Linewidth',1.5,'linesmoothing','on')
plot(handles.veltri_st1,X2,Y2,'r-','Linewidth',1.5,'linesmoothing','on')
plot(handles.veltri_st1,X3,Y3,'b-','Linewidth',1.5,'linesmoothing','on')
plot(handles.veltri_st1,X4,Y4,'k-','Linewidth',1.5,'linesmoothing','on')
plot(handles.veltri_st1,X5,Y5,'r--','Linewidth',1.5,'linesmoothing','on')
plot(handles.veltri_st1,X6,Y6,'b--','Linewidth',1.5,'linesmoothing','on')
plot(handles.veltri_st1,X7,Y7,'k-','Linewidth',1.5,'linesmoothing','on')
hold off
axes(handles.veltri_last)
title('Last stage')
xlabel('m/s')
ylabel('m/s')
hold on
plot(handles.veltri_last,X8,Y8,'g-','Linewidth',1.5,'linesmoothing','on')
plot(handles.veltri_last,X9,Y9,'r-','Linewidth',1.5,'linesmoothing','on')
plot(handles.veltri_last,X10,Y10,'b-','Linewidth',1.5,'linesmoothing','on')
plot(handles.veltri_last,X11,Y11,'k-','Linewidth',1.5,'linesmoothing','on')
plot(handles.veltri_last,X12,Y12,'r-','Linewidth',1.5,'linesmoothing','on')
plot(handles.veltri_last,X13,Y13,'b-','Linewidth',1.5,'linesmoothing','on')
plot(handles.veltri_last,X14,Y14,'k-','Linewidth',1.5,'linesmoothing','on')
hold off
% --- Executes on button press in pushbutton2.
function pushbutton2_Callback(hObject, eventdata, handles)
% hObject
handle to pushbutton2 (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
122
% handles
structure with handles and user data
set(handles.Angles,'visible','off');
set(handles.Rad_Ma,'visible','on');
set(handles.uipanel12,'visible','off')
% --- Executes on button press in pushbutton3.
function pushbutton3_Callback(hObject, eventdata,
% hObject
handle to pushbutton3 (see GCBO)
% eventdata reserved - to be defined in a future
% handles
structure with handles and user data
set(handles.Angles,'visible','on');
set(handles.Rad_Ma,'visible','off');
set(handles.uipanel12,'visible','off')
(see GUIDATA)
handles)
version of MATLAB
(see GUIDATA)
% --- Executes on button press in update.
function update_Callback(hObject, eventdata, handles)
% hObject
handle to update (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
global EXPORT_VALUES
set(handles.h04,'String',EXPORT_VALUES(1)/10^3);
set(handles.P04,'String',EXPORT_VALUES(4)/10^2);
set(handles.s04,'String',EXPORT_VALUES(2)/10^3);
set(handles.T04,'String',EXPORT_VALUES(3));
set(handles.P05,'String',EXPORT_VALUES(9)/10^2);
set(handles.s05,'String',EXPORT_VALUES(7)/10^3);
set(handles.mass,'String',EXPORT_VALUES(10));
set(handles.text337,'string',EXPORT_VALUES(11));
set(handles.text334,'string',EXPORT_VALUES(12));
Vratio = EXPORT_VALUES(12)/EXPORT_VALUES(11)
set(handles.text340,'string',Vratio);
% --- Executes on button press in performance.
function performance_Callback(hObject, eventdata, handles)
% hObject
handle to performance (see GCBO)
% eventdata reserved - to be defined in a future version of MATLAB
% handles
structure with handles and user data (see GUIDATA)
set(handles.Angles,'visible','off');
set(handles.uipanel12,'visible','on')
set(handles.Rad_Ma,'visible','off')
9.2 Turbine calculation
%##########################################################################
%##
##
%##
Turbine Calculation
##
%##
Mikael Olsson
##
%##
##
%##########################################################################
function [n_stage Psi Reac_vek Cx1 C1 C2 C3 W2 W3 M1 M2 M3 M3_rel
station1_height str_height rot_height alfa2 alfa3 beta2 beta3]=...
Turbine(Psi_def,Phi_def,Reac_def,N,U_m,r_m,mass,s1_def,h01_def,T01_def,P01_
def,P0kond_def,T0kond_def,s0kond_def,amne);
%i=1;
Phi = Phi_def
123
n_stage= 1;
Psi(n_stage)=zeros;
Cx1 = Phi*U_m;
AVR=1;
Nue=1;
s1(1) = s1_def;
h01(1) = h01_def;
T01(1) = T01_def;
P01(1) = P01_def;
alfa1(1) = 0;
a01 = refpropm('a','h',h01,'s',s1,char(amne));
M01 = Cx1/a01;
P0kond =
T0kond =
s0kond =
h0kond =
s0kond_s
P0kond_def;
T0kond_def;
s0kond_def;
refpropm('H','T',T0kond,'s',s0kond,char(amne));
= s1_def;
P2_diffuser = P0kond;
C1(1) = Cx1;
h1(1) = h01(1)-C1(1)^2/2;
if n_stage ==1
n_stage = n_stage;
single = 1;
else
n_stage=n_stage-1;
single = 0;
end
Psi(n_stage)=100;
while Psi(n_stage)>Psi_def
%Psi = 2;
if single ==1
n_stage = n_stage;
single = 0;
else
n_stage = n_stage+1;
single = 0;
end
alfa1=0;
h1 = 0;
h01= 0;
s1 = 0;
C1 = 0;
W1 = 0;
s1(1) = s1_def;
h01(1) = h01_def;
T01(1) = T01_def;
P01(1) = P01_def;
alfa1(1) = 0;
C1(1) = Cx1;
h1(1) = h01(1)-(C1(1)^2)/2;
Reac=Reac_def;
124
for i=1:n_stage
Psi(i)=Psi_def;
if i<n_stage
error=0;
[alfa2(i) alfa3(i) beta2(i) beta3(i)
Reac]=ORC_Veltri(Phi,Psi(i),Reac,AVR,Nue,2);
[I2(i) C2(i) C3(i) W2(i) W3(i) verk_tt(i) P1(i) P01(i) P2(i) P02(i)
P02_rel(i) P3(i) P03(i) P03_rel(i) a3(i) T1(i) T01(i) h3(i) h03(i) h03ss(i)
h3ss(i) s2(i) s3(i) kappa3(i) Cp1(i) Cp3(i) M1(i) M2(i) M2_rel(i) M3(i)
M3_rel(i) Ytot_str(i) Ytot_rot(i) HONB_str(i) HONB_rot(i) SONC_str(i)
SONC_rot(i)...
r_tip_str(i) r_tip_rot(i) r_hub_str(i) r_hub_rot(i) r1tip(i)
r1hub(i) V_flow1(i) V_flow2(i) V_flow3(i) fail_str fail_rot b_str(i)
b_rot(i) num_blades_str(i)]=
Calc(alfa2(i),alfa3(i),beta2(i),beta3(i),AVR,mass,alfa1(i),h1(i),h01(i),s1(
i),C1(i),Cx1,U_m,r_m,s0kond_s,char(amne));
Reac_vek(i) = Reac;
elseif i==n_stage
error = 1;
n = 0;
while abs(error)>1/10^2
[alfa2(i) alfa3(i) beta2(i) beta3(i)
Reac]=ORC_Veltri(Phi,Psi(i),Reac,AVR,Nue,1);
[I2(i) C2(i) C3(i) W2(i) W3(i) verk_tt(i) P1(i) P01(i) P2(i)
P02(i) P02_rel(i) P3(i) P03(i) P03_rel(i) a3(i) T1(i) T01(i) h3(i) h03(i)
h03ss(i) h3ss(i) s2(i) s3(i) kappa3(i) Cp1(i) Cp3(i) M1(i) M2(i) M2_rel(i)
M3(i) M3_rel(i) Ytot_str(i) Ytot_rot(i) HONB_str(i) HONB_rot(i) SONC_str(i)
SONC_rot(i)...
r_tip_str(i) r_tip_rot(i) r_hub_str(i) r_hub_rot(i)
r1tip(i) r1hub(i) V_flow1(i) V_flow2(i) V_flow3(i) fail_str fail_rot
b_str(i) b_rot(i) num_blades_str(i)]=
Calc(alfa2(i),alfa3(i),beta2(i),beta3(i),AVR,mass,alfa1(i),h1(i),h01(i),s1(
i),C1(i),Cx1,U_m,r_m,s0kond_s,char(amne));
Reac_vek(i) = Reac;
Cp = (Cp1(i)+Cp3(i))/2;
kappa = kappa3(i);
cp = 0.6; %diffuser koeff.
M1_diffuser=M3(i);
P1_diffuser = P2_diffuser/(1+cp*((1+((kappa1)/2)*M1_diffuser^2)^(kappa/(kappa-1))-1))
error = (P3(i)-P1_diffuser)/10^2;
RLX = 0.30;
dPsi_dP3 = -(1/U_m^2)*((kappa1)/kappa*Cp*verk_tt(i)*T01(i)*(P01(i)/10^2)^((1kappa)/kappa)*(P03(i)/10^2)^(-1/kappa));
Psi(i) = Psi(i)-RLX*error/dPsi_dP3;
if n>=10 && Psi(i)>3
break
125
end
if fail_str==1 || fail_rot==1
break
end
n = n+1;
aa(n)=error;
disp(Psi(i))
end
if fail_str==1 || fail_rot==1
break
end
end
Ns(i)=sqrt(Phi)/(Psi(i))^(3/4)
NS(i)=(N/60)*sqrt(V_flow3(i))/(Psi(i)*U_m^2)^(3/4)
VH(i)= sqrt(V_flow3(i))/(Psi(i)*U_m^2)^(1/4)
VR(i)= V_flow3(i)/V_flow1(i);
w_stage(i) = (h01(i)-h03(i))/10^3;
PWR_stage(i) = mass*w_stage(i);
if (i+1)<=n_stage
alfa1(i+1)=-alfa3(i);
h1(i+1) = h3(i);
h01(i+1)= h03(i);
s1(i+1) = s3(i);
C1(i+1) = C3(i);
W1(i+1) = W3(i);
end
Ygreen_str(i) = (P01(i)-P02(i))/(P02(i)-P2(i));
Ygreen_rot(i) = (P02_rel(i)-P03_rel(i))/(P03_rel(i)-P3(i));
end
end
for j=1:n_stage
if M2(j)>1.4
warndlg('M2 greater than 1.4','Mach warning')
end
if M3_rel(j)>1.4
warndlg('M3_rel greater than 1.4','Mach warning')
end
end
str_height = r_tip_str-r_hub_str;
rot_height = r_tip_rot-r_hub_rot;
station1_height = r1tip- r1hub;
W_turb=0;
126
for i=1:n_stage
W_turb = (W_turb+PWR_stage(i))
end
effic = (h01(1)-h03(n_stage))/(h01(1)-h3ss(n_stage))
9.3 Stage calculation
%##########################################################################
%##
##
%##
Stage Calculation
##
%##
Mikael Olsson
##
%##
##
%##########################################################################
function [I2 C2 C3 W2 W3 verk_tt P1 P01 P2 P02 P02_rel P3 P03 P03_rel a3 T1
T01 h3 h03 h03ss h3ss s2 s3 kappa3 Cp1 Cp3 M1 M2 M2_rel M3 M3_rel Ytot_str
Ytot_rot HONB_str HONB_rot SONC_str SONC_rot...
r_tip_str r_tip_rot r_hub_str r_hub_rot r1tip r1hub V_flow1 V_flow2
V_flow3 fail_str fail_rot b_str b_rot
num_blades_str]=Calc(alfa2,alfa3,beta2,beta3,AVR,mass,alfa1,h1,h01,s1,C1,Cx
1,U_m,r_m,s0kond_s,amne)
[a1 rau1 P1 T1 Cp1 kappa]= refpropm('ADPTCK','H',h1,'s',s1,char(amne));
[P01 T01] =refpropm('PT','H',h1+C1^2/2,'s',s1,char(amne));
M1 = C1/a1;
V_flow1 = mass/rau1;
A1 = mass/(rau1*Cx1); %Annulus
kappa1 = kappa;
r1tip = (A1/(4*pi*r_m))+r_m;
r1hub = 2*r_m-r1tip;
C2 = Cx1/cosd(alfa2);
W2 = Cx1/cosd(beta2);
error = 1;
ds_old = 0;
h02=h01;
h2 = h02-C2^2/2;
raknare_str = 0;
disp('------------------------')
disp(h2)
if h2<0
errordlg('Static enthalpy station 2 negative, C2 to high. Decrease
axial speed or alfa2','Error','on')
end
while abs(error)>0.1
ds_str = ds_old+0.9*error;
s2=s1+ds_str;
if h2<0
keyboard
end
kappa = refpropm('K','H',h2,'s',s2,char(amne));
P2 = refpropm('P','H',h2,'s',s2,char(amne));
P02_rel = refpropm('P','H',h2+W2^2/2,'s',s2,char(amne));
[P02 T02] = refpropm('PT','H',h02,'s',s2,char(amne));
127
[T2 rau2 a2 viskositet] = refpropm('TDAV','H',h2,'s',s2,char(amne));
V_flow2 = mass/rau2;
A2 = mass/(rau2*Cx1);
r_tip_str = (A2/(4*pi*r_m))+r_m;
r_hub_str = 2*r_m-r_tip_str;
M2 = C2/a2;
NorR = 1; %Stator
Ang_in = alfa1;
Ang_in_b = Ang_in;
Desinc = 0;
Ang_out = alfa2;
Ma_in = M1;
Ma_out = M2;
Ps_in = P1;%kPa
Ps_out = P2;%kPa
kappa2 = kappa;
Ang_stagger = stagger1(alfa1,alfa2);
TONC = TONC1(alfa1,alfa2);
[SONC_str SONB Z] = ZweiStaSBC1(alfa1,alfa2,1,Ma_out,AVR,TONC,Ang_stagger); %model ZweiStaSBC1
HTRAT = r_hub_str/r_tip_str;
if SONC_str<0
keyboard
end
fail_str = 0;
if HTRAT<0
fail_str = 1;
%keyboard
errordlg('Negative hub tip ratio for stator, either increase mean
radius or increase Phi','Error','on')
return
end
HONB_str = lonb1(HTRAT,'str');% = modell lonb1
b_str = (r_tip_str-r_hub_str)/HONB_str;%Axial chord
c_str = b_str/cosd(Ang_stagger); %blade chord
Re_str = C2*c_str*rau2/viskositet;
TEONO = 0.01;
HONC = (r_tip_str-r_hub_str)/c_str;%
CLONH = 0.01;
Nseal = 5;
TRmRAT = r_tip_str/r_m;
DLEONC = 0.2;
[Ytot_str,Yp_str,YTE_str,Ys_str,Yclr_str,Ypi_str,YsONYs_DES_str,SONC2_str]=
AMDCKOMK(NorR,Ang_in,Ang_in_b,Desinc,Ang_out,AVR,Ma_in,Ma_out,Ps_in,Ps_out,
Re_str,kappa,SONC_str,TONC,HTRAT,TEONO,HONC,HONB_str,CLONH,Nseal,TRmRAT,DLE
ONC,Ang_stagger,0);
128
Molar = refpropm('M','H',h2,'s',s2,char(amne));
R=1000*(8.314472/Molar);
ds_old = ds_str;
ds_new = -R*log(1-Ytot_str*(P02-P2)/P01); %gibbs: s2-s1=-R*ln(1(deltaP/P1), deltaP = Ytot*(P02-P2)
error = ds_new-ds_old;
raknare_str = raknare_str+1;
error_mth(raknare_str)=error;
if raknare_str>100
disp('stator iteration has failed')
end
fail_str=0;
end
num_blades_str = r_m*2*pi/(SONC_str*c_str)
if beta3<0
beta3_banan = -beta3;
alfa3_banan = -alfa3;
else
beta3_banan = -beta3;
end
I2
C3
W3
h3
=
=
=
=
h2+W2^2/2-U_m^2/2;
Cx1/cosd(alfa3);
Cx1/cosd(beta3);
I2-W3^2/2+U_m^2/2; %Rothalpy const.
error = 10; %ds_ny-ds_gammal
ds_old = 0;
raknare_rot = 0;
Ytot_rot = 0;
while abs(error)>0.1
ds_rot = ds_old+0.9*error;
s3 = s2+ds_rot;
h03 = h3+C3^2/2;
fel =0;
[P03 T03]=refpropm('PT','H',h03,'s',s3,char(amne));
h03_rel=h3+W3^2/2;
[P03_rel T03_rel]=refpropm('PT','H',h03_rel,'s',s3,char(amne));
h03ss_rel = refpropm('H','P',P03_rel,'s',s0kond_s,char(amne));
[P3 Molar] = refpropm('PM','H',h3,'s',s3,char(amne));
T3 = refpropm('T','H',h3,'s',s3,char(amne));
h3ss = refpropm('H','P',P3,'s',s0kond_s,char(amne));
h03ss = refpropm('H','P',P03,'s',s0kond_s,char(amne));
129
rau3 = refpropm('D','H',h3,'s',s3,char(amne));
a3 = refpropm('A','H',h3,'s',s3,char(amne));
viskositet = refpropm('V','H',h3,'s',s3,char(amne));
V_flow3 = mass/rau3;
A3 = mass/(rau3*Cx1);
r_tip_rot = A3/(4*pi*r_m)+r_m;
r_hub_rot = 2*r_m-r_tip_rot;
M2_rel = W2/a2;
M3_rel = W3/a3;
M3 = C3/a3;
NorR = 2; %Rotor
Ang_in = beta2;
Ang_in_b = Ang_in;
Desinc = 0;
Ang_out = beta3_banan;
Ma_in = M2_rel;
Ma_out = M3_rel;
Ps_in = P2;%kPa
Ps_out = P3;%kPa
kappa = refpropm('K','H',h3,'s',s3,char(amne));
kappa3 = kappa;
Ang_stagger = stagger1(beta2,beta3_banan);
TONC = TONC1(beta2,beta3_banan);
[SONC_rot SONB Z] = ZweiStaSBC1(beta2,beta3_banan,1,Ma_out,AVR,TONC,Ang_stagger);
HTRAT = r_hub_rot/r_tip_rot;
fail_rot = 0;
if SONC_rot<0
keyboard
end
if HTRAT<0
fail_rot = 1;
errordlg('Negative hub tip ratio for rotor, either increase mean
radius or increase Phi','Error','on')
return
end
HONB_rot = lonb1(HTRAT,'rtr');% = modell lonb1
b_rot = (r_tip_rot-r_hub_rot)/HONB_rot;%Axial chord
c_rot = b_rot/cosd(Ang_stagger); %blade chord
Re_rot = W3*c_rot*rau3/viskositet;
TEONO = 0.01;
HONC = (r_tip_rot-r_hub_rot)/c_rot;%
CLONH = 0.01;
Nseal = 5;%????
TRmRAT = r_tip_rot/r_m;
DLEONC = 0.2;%???? 0.065
kappa = (kappa2+kappa3)/2;
if Ytot_rot<0
fel =1;
disp(s3-s2)
disp(Ytot_rot)
disp(Yp_rot)
end
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[Ytot_rot,Yp_rot,YTE_rot,Ys_rot,Yclr_rot,Ypi_rot,YsONYs_DES_rot,SONC2_rot]=
AMDCKOMK(NorR,Ang_in,Ang_in_b,Desinc,Ang_out,AVR,Ma_in,Ma_out,Ps_in,Ps_out,
Re_rot,kappa,SONC_rot,TONC,HTRAT,TEONO,HONC,HONB_rot,CLONH,Nseal,TRmRAT,DLE
ONC,Ang_stagger,fel);
Cp3 = refpropm('C','H',h3,'s',s3,char(amne));
Cv = refpropm('O','H',h3,'s',s3,char(amne));
R=1000*(8.314472/Molar);
ds_old = ds_rot;
ds_new = -R*log(1-Ytot_rot*(P03_rel-P3)/P02_rel);
error = ds_new-ds_old;
%verk_tt(i) = (h1-h3)/(h1-h03ss);
verk_tt = (h01-h03)/(h01-h03ss);
%verk_ts(i) = (h01(i)-h03(i))/(h01(i)-h3ss(i));
raknare_rot = raknare_rot+1;
s_koll(raknare_rot) = ds_rot;
error_koll(raknare_rot)=error;
if raknare_rot>100
disp('rotor iteration has failed')
end
fail_rot=0;
end
Ygreen_str = (P01-P02)/(P02-P2);
Ygreen_rot = (P02_rel-P03_rel)/(P03_rel-P3);
fail=0;
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10 Appendix C
10.1 How to connect REFPROP to MATLAB
1. Firstly make sure that refprop is installed on the computer that’s to be used. If not install it
(preferably in C:\Program Files for reasons found in point 3)
2. Go to this address (as of june 2012):
http://www.boulder.nist.gov/div838/theory/refprop/Frequently_asked_questions.htm#Updates
and download the zip file ML2010A.zip containing m files for REFPROP connection to
Matlab. Unpack it where you want but it must be in Matlabs path. Either unpack in the Matlab
working folder or add the chosen folder to path later in Matlab.
3. If REFPROP has been installed in another path than C:\Program Files\REFPROP changes needs
to be made to the downloaded files. How to do this is found in the REFPROP FAQ. It’s
recommended however to install in the program files directory if possible. This has to do with
that the m files is set to search the fluids in that folder and changing the path require some
programming skills.
4. Make sure that the folder with the unpacked files is in the Matlab working directory and then
type: “help refpropm” in the command window. If properly added the window now should
show information about what values refprop returns an also some examples of how to use it.
5. If point 4 do not work check installation of refprop. Is the folder correct? Has the REFPROP
m files been added to the Matlab path?
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