definition of units -...

EG

16.043

28.013

64.063

44.010

26.038

28.054

30.07

44.097

18.015

34.080

2.016

28.010

31.999

58.123

58.123

72.15

72.15

86.177

100.204

114.231

4.0026

39.948

190.6

126.2

430.8

304.2

308.3

282.4

305.4

369.8

647.3

373.2

33.2

132.9

154.6

408.2

425.2

460.4

469.7

507.5

540.3

568.8

5.19

150.8

46.0

33.9

78.8

73.8

61.4

50.4

48.8

42.4

220.9

89.4

13

35.0

50.5

36.5

38

33.9

33.7

30.1

27.4

24.9

2.27

48.7

1.315

1.4

1.27

1.295

1.23

1.24

1.18

1.13

1.33

1.32

1.412

1.395

1.397

1.11

1.1

1.076

1.07

1.062

1.052

1.046

1.66

1.668

:=NG

16.043

28.0135

64.063

44.01

26.038

28.054

30.07

44.097

18.015

34.082

2.0159

28.01

31.9988

58.123

58.123

72.15

72.15

86.177

100.204

114.231

4.0026

39.948

343.1

227.2

775.4

547.6

554.9

508.3

549.7

665.6

1165.1

671.8

59.8

239.2

278.3

734.6

765.4

828.7

845.3

913.3

972.4

1023.8

9.34

271.4

667.2

492.3

1142.9

1069.9

890.5

731

708.4

615.8

3203.9

1269.2

188.1

507

731.9

529.1

551.1

490.9

489.4

430.6

396.8

360.1

32.9

706.9

1.315

1.4

1.27

1.295

1.23

1.24

1.18

1.13

1.33

1.32

1.412

1.395

1.397

1.11

1.1

1.076

1.07

1.062

1.052

1.046

1.66

1.668

:=Comp

"Methane (CH4)"

"Nitrogen (N2)"

"Sulfur Dioxide (SO2)"

"Carbon Dioxide (CO2)"

"Acetylene (C2H2)"

"Ethene (C2H4)"

"Ethane (C2H6)"

"Propane (C3H8)"

"Water (H20)"

"Hydrogen Sulfide (H2S)"

"Hydrogen (H2)"

"Carbon Monoxide (CO)"

"Oxygen (O2)"

"i-Butane (C4H10)"

"n-Butane (C4H10)"

"i-Pentane (C5H12)"

"n-Pentane (C5H12)"

"n-Hexane (C6H14)"

"n-Heptane (C7H16)"

"n-Octane (C8H18)"

"Helium (He)"

"Argon (Ar)"

100

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

:=

EG<3> k [-]NG<3> k [-]

EG<2> Pc [bara]NG<2> Pc [psia]

EG<1> Tc [K]NG<1> Tc [°R]Comp<1> Tc [°R]

EG<0> M [kg/kmol]NG<0> M [kg/kmol]Comp<0> Comp [-]

Source:

VDI Wärmeatlas

Gas Composition Data

Fuel Gas Composition:

The following Gas Composition Data is calculated based on the DCCD listed composition of 98% Methane, 1.4%

Nitrogen, and 0.6% Ethane. The Z-factor is computed using the Redlich-Kwong Compressibility Factor Equation

as defined in the Flow Measurement Engineering Handbook.

Definition of Units

krk 1.315=

krk k0

Cfrac0

⋅ k1

Cfrac1

⋅+ k2

Cfrac2

⋅+ k3

Cfrac3

⋅+ k4

Cfrac4

⋅+ k5

Cfrac5

⋅+ k6

Cfrac6

⋅+ k7

Cfrac7

⋅+ k8

Cfrac8

⋅+

k9

Cfrac9

⋅ k10

Cfrac10

⋅+ k11

Cfrac11

⋅+ k12

Cfrac12

⋅+ k13

Cfrac13

⋅+ k14

Cfrac14

⋅+ k15

Cfrac15

⋅++

...

k16

Cfrac16

⋅ k17

Cfrac17

⋅+ k18

Cfrac18

⋅+ k19

Cfrac19

⋅+ k20

Cfrac20

⋅+ k21

Cfrac21

⋅++

...

1⋅:=

Specific Heats for Fuel Gas Composition:

Pcrk 46 bar=

Pcrk Pc0

Cfrac0

⋅ Pc1

Cfrac1

⋅+ Pc2

Cfrac2

⋅+ Pc3

Cfrac3

⋅+ Pc4

Cfrac4

⋅+ Pc5

Cfrac5

⋅+ Pc6

Cfrac6

⋅+ Pc7

Cfrac7

⋅+

Pc8

Cfrac8

⋅ Pc9

Cfrac9

⋅+ Pc10

Cfrac10

⋅+ Pc11

Cfrac11

⋅+ Pc12

Cfrac12

⋅+ Pc13

Cfrac13

⋅+ Pc14

Cfrac14

⋅++

...

Pc15

Cfrac15

⋅ Pc16

Cfrac16

⋅+ Pc17

Cfrac17

⋅+ Pc18

Cfrac18

⋅+ Pc19

Cfrac19

⋅+ Pc20

Cfrac20

⋅+ Pc21

Cfrac21

⋅++

...

1⋅ bar:=

Critical Pressure for Fuel Gas Composition:Tcrk 190.6 K=

Tcrk Tc0

Cfrac0

⋅ Tc1

Cfrac1

⋅+ Tc2

Cfrac2

⋅+ Tc3

Cfrac3

⋅+ Tc4

Cfrac4

⋅+ Tc5

Cfrac5

⋅+ Tc6

Cfrac6

⋅+ Tc7

Cfrac7

⋅+

Tc8

C%8

⋅ Tc9

C%9

⋅+ Tc10

C%10

⋅+ Tc11

C%11

⋅+ Tc12

C%12

⋅+ Tc13

C%13

⋅+ Tc14

C%14

⋅++

...

Tc15

Cfrac15

⋅ Tc16

Cfrac16

⋅+ Tc17

Cfrac17

⋅+ Tc18

Cfrac18

⋅+ Tc19

Cfrac19

⋅+ Tc20

Cfrac20

⋅+ Tc21

Cfrac21

⋅++

...

1⋅ K⋅:=

Critical Temperature for Fuel Gas Composition:

Mrk 16.043kg

kmol=

Mrk M0

Cfrac0

⋅ M1

Cfrac1

⋅+ M2

Cfrac2

⋅+ M3

Cfrac3

⋅+ M4

Cfrac4

⋅+ M5

Cfrac5

⋅+ M6

Cfrac6

⋅+ M7

Cfrac7

⋅+

M8

Cfrac8

⋅ M9

Cfrac9

⋅+ M10

Cfrac10

⋅+ M11

Cfrac11

⋅+ M12

Cfrac12

⋅+ M13

Cfrac13

⋅+ M14

Cfrac14

⋅++

...

M15

Cfrac15

⋅ M16

Cfrac16

⋅+ M17

Cfrac17

⋅+ M18

Cfrac18

⋅+ M19

Cfrac19

⋅+ M20

Cfrac20

⋅+ M21

Cfrac21

⋅++

...

1⋅kg

kmol:=

Molecular Weight for Fuel Gas Composition:

Sum_frac 1=

Sum_frac Cfrac0

Cfrac1

+ Cfrac2

+ Cfrac3

+ Cfrac4

+ Cfrac5

+ Cfrac6

+ Cfrac7

+ Cfrac8

+ Cfrac9

+ Cfrac10

+ Cfrac11

+

Cfrac12

Cfrac13

+ Cfrac14

+ Cfrac15

+ Cfrac16

+ Cfrac17

+ Cfrac18

+ Cfrac19

+ Cfrac20

+ Cfrac21

++

...:=

Sum_% 100=

Sum_% C%0

C%1

+ C%2

+ C%3

+ C%4

+ C%5

+ C%6

+ C%7

+ C%8

+ C%9

+ C%10

+ C%11

+ C%12

+

C%13

C%14

+ C%15

+ C%16

+ C%17

+ C%18

+ C%19

+ C%20

+ C%21

++

...:=

Sum of Fuel Gas mol-% and Fuel Gas Fraction respectively:

k EG3⟨ ⟩

:=Pc EG2⟨ ⟩

:=Tc EG1⟨ ⟩

:=M EG0⟨ ⟩

:=C% Comp

1⟨ ⟩:=Cfrac

Comp1⟨ ⟩

100:=

Definition of variables and assignments of matrix columns:

CALCULATIONS:

ρ 1.01325 bar⋅ 273.15 K⋅,( ) 0.716kg

m3

=

ρ p T,( )p

Zrk p T,( ) Ri⋅ T⋅REAL 1=if

p

Ri T⋅otherwise

:=

RiR

Mrk

:=

REAL 0=

CheckBox:

• Activate CheckBox to perform your calcs with Redlich-Kwong Gas Compressibility Factor Z

• Otherwise cals will be performed without Redlich-Kwong Gas Compressibility Factor Z

Ideal Gas Equation resolved with the Redlich-Kwong Gas Compressibility Factor Zrk:

Ideal Gas Equation resolved without the Redlich-Kwong Gas Compressibility Factor Zrk:

Zrk 1.01325 bar⋅ 273.15 K⋅,( ) 0.9975=Zrk P T,( ) Suchen Z( ):=

RK P T, Z,( ) 0=

Vorgabe

Z 1:=

The Redlich-Kwong Equation-of-State is non-linear requiring an iterative solution. The solution will be left

as a function of Pressure and Temperature:

RK P T, Z,( ) Z3

Z2

− B P T,( )2

B P T,( )+ A P T,( )−( ) Z⋅− A P T,( ) B P T,( )⋅−:=

Redlich-Kwong Equation-of-State as a function of Pressure, Temperature and Compressibility Factor Z:

B P T,( )0.086647 Pr P( )⋅

Tr T( ):=A P T,( )

0.42748 Pr P( )⋅

Tr T( )( )2.5

:=

Redlich-Kwong Constants as functions of Pressure P and Temperature T:

Tr T( )T

Tcrk

:=Pr P( )P

Pcrk

:=

Reduced Pressure Pr and Reduced Temperature Tr as functions:

Redlich-Kwong Equation for a given Gas Composition

Viscosity of Natural Gas:

Fuel Gas Systems operates below 1500 psia (103.43 bara), so all pressure effects on viscosity are neglected. A

temperature correction for viscosity is used, taken from the Flow Measurement Engineering Handbook (equation

2.246).

η T( ) 0.0098459.67 0.9 Tcrk⋅+

T 459.67+( ) 0.9 Tcrk⋅+

⋅T 459.67+

459.67

1.5

⋅ centipoise⋅:=

η T( ) 1.098 105−

⋅ Pa⋅ s⋅273.15 K⋅ 165 K⋅+( )

T 165 K⋅+( )⋅

T

273.15 K⋅

1.5

⋅:=

p82 20 bar⋅:=p72 20 bar⋅:=

p62 20 bar⋅:=p52 20 bar⋅:=p42 20 bar⋅:=p32 20 bar⋅:=p22 20 bar⋅:=p12 20 bar⋅:=

pcc 20 bar⋅:=Pressure at Combustion Chamber pcc

T 488.15 K⋅:=

Fuel Gas Temperature

m° 0.50 m°A⋅:=m°A 0.37 26⋅kg

s⋅:=

Mass Flows

Process Data of Fuel Gas:

λI λJ λK λL

λ1 λ2 λ3 λ4 λ5 λ6 λ7 λ8 λ9 λ10 λ11 λ12

Given:

κ krk:=

ηL η T( ):=ηK η T( ):=ηJ η T( ):=ηI η T( ):=ηH η T( ):=

ηG η T( ):=ηF η T( ):=ηE η T( ):=ηD η T( ):=ηC η T( ):=ηB η T( ):=ηA η T( ):=

η12 η T( ):=η11 η T( ):=

p92 20 bar⋅:= p102 20 bar⋅:= p112 20 bar⋅:= p122 20 bar⋅:=

Physical Properties of Fuel Gas:

Dynamic Viscosities:

η0 η T( ):= η1 η T( ):= η2 η T( ):= η3 η T( ):= η4 η T( ):= η5 η T( ):= η6 η T( ):=

η7 η T( ):= η8 η T( ):= η9 η T( ):= η10 η T( ):=

Inlet pressures at individual feeder lines including manifold / feeder line tee fitting:

p12p11p10p9p8p7p6p5p4p3p2p1

Inlet pressures at individual feeder lines:

p0p

Manifold Solution SGT5-8000H

Find:

Mass flows at each individual feeder line:

m°1 m°2 m°3 m°4 m°5 m°6 m°7 m°8 m°9 m°10 m°11 m°12

Required supply pressure p at manifold inlet tee fitting and pressure p0 downstream inlet tee fitting:

p5B p6B p7B p8B p9B p10B p11B p12B

Friction factors at individual manifold sections:

λA λB λC λD λE λF λG λH

p1a p2a p3a p4a p5a p6a p7a p8a p9a p10a p11a p12a

Upstream pressures at each individual burner:

p1B p2B p3B p4B

d0 0.200 m⋅:=

Diameters of GT Manifold Piping at each Piping Section

l12 10.0 m⋅:=l11 10.0 m⋅:=l10 10.0 m⋅:=l9 10.0 m⋅:=

l8 10.0 m⋅:=l7 10.0 m⋅:=l6 10.0 m⋅:=l5 10.0 m⋅:=l4 10.0 m⋅:=l3 10.0 m⋅:=l2 10.0 m⋅:=l1 10.0 m⋅:=

Length of Feeder Lines

lK 1.2 m⋅:=lJ 1.2 m⋅:=lI 1.2 m⋅:=lH 1.2 m⋅:=

lG 1.2 m⋅:=lF 1.2 m⋅:=lE 1.2 m⋅:=lD 1.2 m⋅:=

kK 0.0002 m⋅:=kJ 0.0002 m⋅:=kI 0.0002 m⋅:=kH 0.0002 m⋅:=kG 0.0002 m⋅:=kF 0.0002 m⋅:=

dK 0.200 m⋅:=dJ 0.200 m⋅:=dI 0.200 m⋅:=dH 0.200 m⋅:=dG 0.200 m⋅:=dF 0.200 m⋅:=

kE 0.0002 m⋅:=kD 0.0002 m⋅:=kC 0.0002 m⋅:=kB 0.0002 m⋅:=kA 0.0002 m⋅:=k0 0.0002 m⋅:=

dE 0.200 m⋅:=dD 0.200 m⋅:=dC 0.200 m⋅:=dB 0.200 m⋅:=dA 0.200 m⋅:=

ζd6 0.0:=ζd5 0.0:=ζd4 0.0:=ζd3 0.0:=ζd2 0.0:=ζd1 0.0:=

10.50.3330.250.200.1670.1430.125

Branch fittings at GT Manifold / Feeder Piping

dT_out 0.200 m⋅:=dT_in 0.200 m⋅:=ζT 0.7:=

Tee at GT Manifold Inlet

Piping Data of GT Manifold Piping and Feeder Lines:

Aeff 1.9 cm2

⋅:=

Aeff is also known as αA parameter given in cm2

Burner Specific Data:

lC 1.2 m⋅:=lB 1.2 m⋅:=lA 1.2 m⋅:=l0 1.2 m⋅:=

Distances between GT Manifold Piping Sections

Data for GT Manifold Piping:

ζa12 0.98:=ζa11 0.98:=ζa10 0.98:=ζa9 0.98:=

ζa8 0.98:=ζa7 0.98:=ζa6 0.98:=ζa5 0.98:=ζa4 0.98:=ζa3 0.98:=ζa2 0.98:=ζa1 0.98:=

ζd12 0.0:=ζd11 0.0:=ζd10 0.0:=ζd9 0.0:=

ζd8 0.0:=ζd7 0.0:=

k12 0.0002 m⋅:=k11 0.0002 m⋅:=k10 0.0002 m⋅:=k9 0.0002 m⋅:=k8 0.0002 m⋅:=

d12 0.050 m⋅:=d11 0.050 m⋅:=d10 0.050 m⋅:=d9 0.050 m⋅:=d8 0.050 m⋅:=

k7 0.0002 m⋅:=k6 0.0002 m⋅:=k5 0.0002 m⋅:=k4 0.0002 m⋅:=k3 0.0002 m⋅:=k2 0.0002 m⋅:=k1 0.0002 m⋅:=

d7 0.050 m⋅:=d6 0.050 m⋅:=d5 0.050 m⋅:=d4 0.050 m⋅:=d3 0.050 m⋅:=d2 0.050 m⋅:=d1 0.050 m⋅:=

Diameter of Feeder Piping

dpT ζTρ

2⋅ w

2⋅:=

The velocity w is related to velocity at fitting inlet

pressure loss of tee fittings

dp0 λ0

l0

d0

⋅ρ

2⋅

4 m°⋅

d02

π⋅ ρ⋅

2

⋅:=

Pressure loss of piping

1

λ0

2− log2.51

4 m°0⋅ d0⋅

d02

π⋅ ρ⋅ ν0⋅

λ0⋅

k0

d0

0.269⋅+

⋅:=

Lambda calculation for turbulent flow

m° m°1 m°1+ ....+ m°n+:=

Mass balance

Gleichungssystem:

η T( ) 1.098 105−

⋅ Pa⋅ s⋅273.15 K⋅ 165 K⋅+( )

T 165 K⋅+( )⋅

T

273.15 K⋅

1.5

⋅:=

η T( ) 0.0098459.67 0.9 Tcrk⋅+

T 459.67+( ) 0.9 Tcrk⋅+

⋅T 459.67+

459.67

1.5

⋅ centipoise⋅:=

Fuel Gas Systems operates below 1500 psia (103.43 bara), so all pressure effects on viscosity are neglected. A

temperature correction for viscosity is used, taken from the Flow Measurement Engineering Handbook (equation

2.246).

Viscosity of Natural Gas:

ρ P T,( )P 144⋅ Mrk⋅

Zrk P T,( ) 1545⋅ T 459.67+( )⋅

lb

ft3

⋅:=

Ideal Gas Equation resolved with the Redlich-Kwong Gas Compressibility Factor Zrk:

ρ p T,( )p

Ri T⋅:=

Ideal Gas Equation:

Herleitung der Formeln

critical condition

non-critical conditionψ p4B pcc, κ,( )κ

κ 1−

pcc

p4B

2

κpcc

p4B

κ 1+

κ

−

⋅pcc

p4B

2

κ 1+

κ

κ 1−

>if

2

κ 1+

1

κ 1−κ

κ 1+⋅

pcc

p4B

2

κ 1+

κ

κ 1−

≤if

:=

Definition of ψ depending on pressure ratio at 4th burner:

critical condition


κ 1−

pcc

p3B

2

κpcc

p3B

κ 1+

κ

−

⋅pcc

p3B

2

κ 1+

κ

κ 1−

>if

2

κ 1+

1

κ 1−κ

κ 1+⋅

pcc

p3B

2

κ 1+

κ

κ 1−

≤if

:=

Definition of ψ depending on pressure ratio at 3rd burner:

critical condition


κ 1−

pcc

p2B

2

κpcc

p2B

κ 1+

κ

−

⋅pcc

p2B

2

κ 1+

κ

κ 1−

>if

2

κ 1+

1

κ 1−κ

κ 1+⋅

pcc

p2B

2

κ 1+

κ

κ 1−

≤if

:=

Definition of ψ depending on pressure ratio at 2nd burner:

critical condition


κ 1−

pcc

p1B

2

κpcc

p1B

κ 1+

κ

−

⋅pcc

p1B

2

κ 1+

κ

κ 1−

>if

2

κ 1+

1

κ 1−κ

κ 1+⋅

pcc

p1B

2

κ 1+

κ

κ 1−

≤if

:=

Definition of ψ depending on pressure ratio at 1st burner:

CALCULATIONS FOR BURNERS:

critical condition


κ 1−

pcc

p8B

2

κpcc

p8B

κ 1+

κ

−

⋅pcc

p8B

2

κ 1+

κ

κ 1−

>if

2

κ 1+

1

κ 1−κ

κ 1+⋅

pcc

p8B

2

κ 1+

κ

κ 1−

≤if

:=


critical condition


κ 1−

pcc

p7B

2

κpcc

p7B

κ 1+

κ

−

⋅pcc

p7B

2

κ 1+

κ

κ 1−

>if

2

κ 1+

1

κ 1−κ

κ 1+⋅

pcc

p7B

2

κ 1+

κ

κ 1−

≤if

:=


critical condition


κ 1−

pcc

p6B

2

κpcc

p6B

κ 1+

κ

−

⋅pcc

p6B

2

κ 1+

κ

κ 1−

>if

2

κ 1+

1

κ 1−κ

κ 1+⋅

pcc

p6B

2

κ 1+

κ

κ 1−

≤if

:=


critical condition


κ 1−

pcc

p5B

2

κpcc

p5B

κ 1+

κ

−

⋅pcc

p5B

2

κ 1+

κ

κ 1−

>if

2

κ 1+

1

κ 1−κ

κ 1+⋅

pcc

p5B

2

κ 1+

κ

κ 1−

≤if

:=


critical condition


κ 1−

pcc

p12B

2

κpcc

p12B

κ 1+

κ

−

⋅pcc

p12B

2

κ 1+

κ

κ 1−

>if

2

κ 1+

1

κ 1−κ

κ 1+⋅

pcc

p12B

2

κ 1+

κ

κ 1−

≤if

:=


critical condition


κ 1−

pcc

p11B

2

κpcc

p11B

κ 1+

κ

−

⋅pcc

p11B

2

κ 1+

κ

κ 1−

>if

2

κ 1+

1

κ 1−κ

κ 1+⋅

pcc

p11B

2

κ 1+

κ

κ 1−

≤if

:=


critical condition


κ 1−

pcc

p10B

2

κpcc

p10B

κ 1+

κ

−

⋅pcc

p10B

2

κ 1+

κ

κ 1−

>if

2

κ 1+

1

κ 1−κ

κ 1+⋅

pcc

p10B

2

κ 1+

κ

κ 1−

≤if

:=


critical condition


κ 1−

pcc

p9B

2

κpcc

p9B

κ 1+

κ

−

⋅pcc

p9B

2

κ 1+

κ

κ 1−

>if

2

κ 1+

1

κ 1−κ

κ 1+⋅

pcc

p9B

2

κ 1+

κ

κ 1−

≤if

:=


p10 20 bar⋅:=p9 20 bar⋅:=p8 20 bar⋅:=p7 20 bar⋅:=

p6 20 bar⋅:=p5 20 bar⋅:=p4 20 bar⋅:=p3 20 bar⋅:=p2 20 bar⋅:=p1 20 bar⋅:=

pa12 20 bar⋅:=pa11 20 bar⋅:=pa10 20 bar⋅:=pa9 20 bar⋅:=pa8 20 bar⋅:=pa7 20 bar⋅:=

pa6 20 bar⋅:=pa5 20 bar⋅:=pa4 20 bar⋅:=pa3 20 bar⋅:=pa2 20 bar⋅:=

p p0− ζTρ p T,( )

2⋅

4 m°A⋅

dT_in2

π⋅ ρ p T,( )⋅

2

⋅=

calculation for pressure loss at manifold inlet tee

m° m°1 m°2+ m°3+ m°4+ m°5+ m°6+ m°7+ m°8+ m°9+ m°10+ m°11+ m°12+=

calculation for mass balance

Gleichungssystem: ... Gleichungen mit ... Unbekannten:

Vorgabe

Lösungsblock:

p12B pcc 1 bar⋅+:=p11B pcc 1 bar⋅+:=

p10B pcc 1 bar⋅+:=p9B pcc 1 bar⋅+:=p8B pcc 1 bar⋅+:=p7B pcc 1 bar⋅+:=p6B pcc 1 bar⋅+:=

p5B pcc 1 bar⋅+:=p4B pcc 1 bar⋅+:=p3B pcc 1 bar⋅+:=p2B pcc 1 bar⋅+:=p1B pcc 1 bar⋅+:=

p12 20 bar⋅:=p11 20 bar⋅:=

λ5 0.015:=λ4 0.015:=λ3 0.015:=λ2 0.015:=λ1 0.015:=

λK 0.015:=λJ 0.015:=λI 0.015:=λH 0.015:=

λG 0.015:=λF 0.015:=λE 0.015:=λD 0.015:=λC 0.015:=λB 0.015:=λA 0.015:=λ0 0.015:=

Schätzwerte für Iteration im Lösungsblock:

Numerische Lösung eines Gleichungssystems mittels Lösungsblock:

BERECHNUNG:

pa1 20 bar⋅:=

p0 21 bar⋅:=p 21.5 bar⋅:=

m°12 0.401kg

s⋅:=m°11 0.401

kg

s⋅:=

m°10 0.401kg

s⋅:=m°9 0.401

kg

s⋅:=m°8 0.401

kg

s⋅:=m°7 0.401

kg

s⋅:=m°6 0.401

kg

s⋅:=

m°5 0.401kg

s⋅:=m°4 0.401

kg

s⋅:=m°3 0.401

kg

s⋅:=m°2 0.401

kg

s⋅:=m°1 0.401

kg

s⋅:=

λ12 0.015:=λ11 0.015:=λ10 0.015:=λ9 0.015:=

λ8 0.015:=λ7 0.015:=λ6 0.015:=

calculation for friction factor at manifold section 0

1

λ0

2− log2.51

4 m°⋅ d0⋅

d02

π⋅ η0⋅

λ0⋅

k0

d0

0.269⋅+

⋅=

calculation for pressure loss at manifold section 0

p0 pa1− λ0

l0

d0

⋅ρ p0 T,( )

2⋅

4 m°⋅

d02

π⋅ ρ p0 T,( )⋅

2

⋅=

calculation for friction factor at manifold section A

1

λA

2− log2.51

4 m° m°1−( )⋅ dA⋅

dA2

π⋅ ηA⋅

λA⋅

kA

dA

0.269⋅+

⋅=

pa1 pa2− λA

lA

dA

⋅ρ pa1 T,( )

2⋅

4 m° m°1−( )⋅

dA2

π⋅ ρ pa1 T,( )⋅

2

⋅=

1

λB

2− log2.51

4 m° m°1− m°2−( )⋅ dB⋅

dB2

π⋅ ηB⋅

λB⋅

kB

dB

0.269⋅+

⋅=

pa2 pa3− λB

lB

dB

⋅ρ pa2 T,( )

2⋅

4 m° m°1− m°2−( )⋅

dB2

π⋅ ρ pa2 T,( )⋅

2

⋅=

1

λC

2− log2.51

4 m° m°1− m°2− m°3−( )⋅ dC⋅

dC2

π⋅ ηC⋅

λC⋅

kC

dC

0.269⋅+

⋅=

pa3 pa4− λC

lC

dC

⋅ρ pa3 T,( )

2⋅

4 m° m°1− m°2− m°3−( )⋅

dC2

π⋅ ρ pa3 T,( )⋅

2

⋅=

1

λD

2− log2.51

4 m° m°1− m°2− m°3− m°4−( )⋅ dD⋅

dD2

π⋅ ηD⋅

λD⋅

kD

dD

0.269⋅+

⋅=

pa4 pa5− λD

lD

dD

⋅ρ pa4 T,( )

2⋅

4 m° m°1− m°2− m°3− m°4−( )⋅

dD2

π⋅ ρ pa4 T,( )⋅

2

⋅=

1

λE

2− log2.51

4 m° m°1− m°2− m°3− m°4− m°5−( )⋅ dE⋅

dE2

π⋅ ηE⋅

λE⋅

kE

dE

0.269⋅+

⋅=

pa5 pa6− λE

lE

dE

⋅ρ pa5 T,( )

2⋅

4 m° m°1− m°2− m°3− m°4− m°5−( )⋅

dE2

π⋅ ρ pa5 T,( )⋅

2

⋅=

1

λF

2− log2.51

4 m° m°1− m°2− m°3− m°4− m°5− m°6−( )⋅ dF⋅

dF2

π⋅ ηF⋅

λF⋅

kF

dF

0.269⋅+

⋅=

pa6 pa7− λF

lF

dF

⋅ρ pa6 T,( )

2⋅

4 m° m°1− m°2− m°3− m°4− m°5− m°6−( )⋅

dF2

π⋅ ρ pa6 T,( )⋅

2

⋅=

1

λG

2− log2.51

4 m° m°1− m°2− m°3− m°4− m°5− m°6− m°7−( )⋅ dG⋅

dG2

π⋅ ηG⋅

λG⋅

kG

dG

0.269⋅+

⋅=

pa7 pa8− λG

lG

dG

⋅ρ pa7 T,( )

2⋅

4 m° m°1− m°2− m°3− m°4− m°5− m°6− m°7−( )⋅

dG2

π⋅ ρ pa7 T,( )⋅

2

⋅=

1

λH

2− log2.51

4 m° m°1− m°2− m°3− m°4− m°5− m°6− m°7− m°8−( )⋅ dH⋅

dH2

π⋅ ηH⋅

λH⋅

kH

dH

0.269⋅+

⋅=

pa8 pa9− λH

lH

dH

⋅ρ pa8 T,( )

2⋅

4 m° m°1− m°2− m°3− m°4− m°5− m°6− m°7− m°8−( )⋅

dH2

π⋅ ρ pa8 T,( )⋅

2

⋅=

1

λI

2− log2.51

4 m° m°1− m°2− m°3− m°4− m°5− m°6− m°7− m°8− m°9−( )⋅ dI⋅

dI2

π⋅ ηI⋅

λI⋅

kI

dI

0.269⋅+

⋅=

pa9 pa10− λI

lI

dI

⋅ρ pa9 T,( )

2⋅

4 m° m°1− m°2− m°3− m°4− m°5− m°6− m°7− m°8− m°9−( )⋅

dI2

π⋅ ρ pa9 T,( )⋅

2

⋅=

1

λJ

2− log2.51

4 m° m°1− m°2− m°3− m°4− m°5− m°6− m°7− m°8− m°9− m°10−( )⋅ dJ⋅

dJ2

π⋅ ηJ⋅

λJ⋅

kJ

dJ

0.269⋅+

⋅=

pa10 pa11− λJ

lJ

dJ

⋅ρ pa10 T,( )

2⋅

4 m° m°1− m°2− m°3− m°4− m°5− m°6− m°7− m°8− m°9− m°10−( )⋅

dJ2

π⋅ ρ pa10 T,( )⋅

2

⋅=

1

λK

2− log2.51

4 m° m°1− m°2− m°3− m°4− m°5− m°6− m°7− m°8− m°9− m°10− m°11−( )⋅ dK⋅

dK2

π⋅ ηK⋅

λK⋅

kK

dK

0.269⋅+

⋅=

pa11 pa12− λK

lK

dK

⋅ρ pa11 T,( )

2⋅

4 m° m°1− m°2− m°3− m°4− m°5− m°6− m°7− m°8− m°9− m°10− m°11−( )⋅

dK2

π⋅ ρ pa11 T,( )⋅

2

⋅=

pa1 p1− ζa1

ρ pa1 T,( )2

⋅4 m°1⋅

d12

π⋅ ρ pa1 T,( )⋅

2

⋅=

1

λ1

2− log2.51

4 m°1⋅ d1⋅

d12

π⋅ η1⋅

λ1⋅

k1

d1

0.269⋅+

⋅=

p1 p1B− λ1

l1

d1

⋅ρ p1 T,( )

2⋅

4 m°1⋅

d12

π⋅ ρ p1 T,( )⋅

2

⋅=

m°1 Aeff ψ p1B pcc, κ,( )⋅ 2 p1B⋅ ρ p1B T,( )⋅⋅=

pa2 p2− ζa2

ρ pa2 T,( )2

⋅4 m°2⋅

d12

π⋅ ρ pa2 T,( )⋅

2

⋅=

1

λ2

2− log2.51

4 m°2⋅ d2⋅

d22

π⋅ η2⋅

λ2⋅

k2

d2

0.269⋅+

⋅=

p2 p2B− λ2

l2

d2

⋅ρ p2 T,( )

2⋅

4 m°2⋅

d22

π⋅ ρ p2 T,( )⋅

2

⋅=


pa3 p3− ζa3

ρ pa3 T,( )2

⋅4 m°3⋅

d12

π⋅ ρ pa3 T,( )⋅

2

⋅=

1

λ3

2− log2.51

4 m°3⋅ d3⋅

d32

π⋅ η3⋅

λ3⋅

k3

d3

0.269⋅+

⋅=

p3 p3B− λ3

l3

d3

⋅ρ p3 T,( )

2⋅

4 m°3⋅

d32

π⋅ ρ p3 T,( )⋅

2

⋅=


pa4 p4− ζa4

ρ pa4 T,( )2

⋅4 m°4⋅

d12

π⋅ ρ pa4 T,( )⋅

2

⋅=

1

λ4

2− log2.51

4 m°4⋅ d4⋅

d42

π⋅ η4⋅

λ4⋅

k4

d4

0.269⋅+

⋅=

p4 p4B− λ4

l4

d4

⋅ρ p4 T,( )

2⋅

4 m°4⋅

d42

π⋅ ρ p4 T,( )⋅

2

⋅=


pa5 p5− ζa5

ρ pa5 T,( )2

⋅4 m°5⋅

d12

π⋅ ρ pa5 T,( )⋅

2

⋅=

1

λ5

2− log2.51

4 m°5⋅ d5⋅

d52

π⋅ η5⋅

λ5⋅

k5

d5

0.269⋅+

⋅=

p5 p5B− λ5

l5

d5

⋅ρ p5 T,( )

2⋅

4 m°5⋅

d52

π⋅ ρ p5 T,( )⋅

2

⋅=


pa6 p6− ζa6

ρ pa6 T,( )2

⋅4 m°6⋅

d12

π⋅ ρ pa6 T,( )⋅

2

⋅=

1

λ6

2− log2.51

4 m°6⋅ d6⋅

d62

π⋅ η6⋅

λ6⋅

k6

d6

0.269⋅+

⋅=

p6 p6B− λ6

l6

d6

⋅ρ p6 T,( )

2⋅

4 m°6⋅

d62

π⋅ ρ p6 T,( )⋅

2

⋅=


pa7 p7− ζa7

ρ pa7 T,( )2

⋅4 m°7⋅

d12

π⋅ ρ pa7 T,( )⋅

2

⋅=

1

λ7

2− log2.51

4 m°7⋅ d7⋅

d72

π⋅ η7⋅

λ7⋅

k7

d7

0.269⋅+

⋅=

p7 p7B− λ7

l7

d7

⋅ρ p7 T,( )

2⋅

4 m°7⋅

d72

π⋅ ρ p7 T,( )⋅

2

⋅=


pa8 p8− ζa8

ρ pa8 T,( )2

⋅4 m°8⋅

d12

π⋅ ρ pa8 T,( )⋅

2

⋅=

1

λ8

2− log2.51

4 m°8⋅ d8⋅

d82

π⋅ η8⋅

λ8⋅

k8

d8

0.269⋅+

⋅=

p8 p8B− λ8

l8

d8

⋅ρ p8 T,( )

2⋅

4 m°8⋅

d82

π⋅ ρ p8 T,( )⋅

2

⋅=


pa9 p9− ζa9

ρ pa9 T,( )2

⋅4 m°9⋅

d12

π⋅ ρ pa9 T,( )⋅

2

⋅=

1

λ9

2− log2.51

4 m°9⋅ d9⋅

d92

π⋅ η9⋅

λ9⋅

k9

d9

0.269⋅+

⋅=

p9 p9B− λ9

l9

d9

⋅ρ p9 T,( )

2⋅

4 m°9⋅

d92

π⋅ ρ p9 T,( )⋅

2

⋅=


pa10 p10− ζa10

ρ pa10 T,( )2

⋅4 m°10⋅

d12

π⋅ ρ pa10 T,( )⋅

2

⋅=

1

λ10

2− log2.51

4 m°10⋅ d10⋅

d102

π⋅ η10⋅

λ10⋅

k10

d10

0.269⋅+

⋅=

p10 p10B− λ10

l10

d10

⋅ρ p10 T,( )

2⋅

4 m°10⋅

d102

π⋅ ρ p10 T,( )⋅

2

⋅=


pa11 p11− ζa11

ρ pa11 T,( )2

⋅4 m°11⋅

d12

π⋅ ρ pa11 T,( )⋅

2

⋅=

1

λ11

2− log2.51

4 m°11⋅ d11⋅

d112

π⋅ η11⋅

λ11⋅

k11

d11

0.269⋅+

⋅=

p11 p11B− λ11

l11

d11

⋅ρ p11 T,( )

2⋅

4 m°11⋅

d112

π⋅ ρ p11 T,( )⋅

2

⋅=


pa12 p12− ζa12

ρ pa12 T,( )2

⋅4 m°12⋅

d12

π⋅ ρ pa12 T,( )⋅

2

⋅=

1

λ12

2− log2.51

4 m°12⋅ d12⋅

d122

π⋅ η12⋅

λ12⋅

k12

d12

0.269⋅+

⋅=

p12 p12B− λ12

l12

d12

⋅ρ p12 T,( )

2⋅

4 m°12⋅

d122

π⋅ ρ p12 T,( )⋅

2

⋅=


λ0_Result

λA_Result

λB_Result

λC_Result

λD_Result

λE_Result

λF_Result

λG_Result

λH_Result

λI_Result

λJ_Result

λK_Result

λ1_Result

λ2_Result

λ3_Result

λ4_Result

λ5_Result

λ6_Result

λ7_Result

λ8_Result

λ9_Result

λ10_Result

λ11_Result

λ12_Result

m°1_Result

m°2_Result

m°3_Result

m°4_Result

m°4_Result

m°5_Result

m°6_Result

m°7_Result

m°8_Result

m°9_Result

m°10_Result

m°11_Result

m°12_Result

pa1_Result

pa2_Result

pa3_Result

pa4_Result

pa5_Result

pa6_Result

pa7_Result

pa8_Result

pa9_Result

pa10_Result

pa11_Result

pa12_Result

p1_Result

p2_Result

p3_Result

p4_Result

p5_Result

p6_Result

p7_Result

p8_Result

p9_Result

p10_Result

p11_Result

p12_Result

p1B_Result

p2B_Result

p3B_Result

p4B_Result

p5B_Result

p6B_Result

suchen λ0 λA, λB, λC, λD, λE, λF, λG, λH, λI, λJ, λK, λ1, λ2, λ3, λ4, λ5, λ8, λ7, λ8, λ9, λ10, λ11, λ12,(:=

p6B_Result

p7B_Result

p8B_Result

p9B_Result

p10B_Result

p11B_Result

p12B_Result

p0_Result

p_Result

CALCULATIONS FOR BURNERS:

Assignment of Flow Conditions at 1st burner:

Condition_1B wennpcc

p1B_Result

2

κ 1+

κ

κ 1−

≤ "critical pressure ratio", "non-critical pressure ratio",

:=Condition_1B wennpcc

p1B_Result

2

κ 1+

κ

κ 1−


:=

Calculation of pressure loss via 5th burner:


p5B_Result

2

κ 1+

κ

κ 1−



p5B_Result

2

κ 1+

κ

κ 1−


:=

Assignment of Flow Conditions at 5th burner:

dp4B bar=dp4Bdp4B p4B_Result pcc−:=dp4B p4B_Result pcc−:=



p4B_Result

2

κ 1+

κ

κ 1−



p4B_Result

2

κ 1+

κ

κ 1−


:=



Calculation of pressure loss via 3rd burner:


p3B_Result

2

κ 1+

κ

κ 1−



p3B_Result

2

κ 1+

κ

κ 1−


:=

Assignment of Flow Conditions at 3rd burner:


Calculation of pressure loss via 2nd burner:


p2B_Result

2

κ 1+

κ

κ 1−



p2B_Result

2

κ 1+

κ

κ 1−


:=

Assignment of Flow Conditions at 2nd burner:


Calculation of pressure loss via 1st burner:

p1B_Result κ 1+ p1B_Result κ 1+




p8B_Result

2

κ 1+

κ

κ 1−



p8B_Result

2

κ 1+

κ

κ 1−


:=





p7B_Result

2

κ 1+

κ

κ 1−



p7B_Result

2

κ 1+

κ

κ 1−


:=





p6B_Result

2

κ 1+

κ

κ 1−



p6B_Result

2

κ 1+

κ

κ 1−


:=



dpA p1_Result p2_Result−:=dpA p1_Result p2_Result−:=

dp2 p2_Result p2B_Result−:=dp2 p2_Result p2B_Result−:=

dpB p2_Result p3_Result−:=dpB p2_Result p3_Result−:=


dpC p3_Result p4_Result−:=dpC p3_Result p4_Result−:=


dpD p4_Result p5_Result−:=dpD p4_Result p5_Result−:=


dpE p5_Result p6_Result−:=dpE p5_Result p6_Result−:=


dpF p6_Result p7_Result−:=dpF p6_Result p7_Result−:=


dpG p7_Result p8_Result−:=dpG p7_Result p8_Result−:=


dp p_Result p0_Result−:=dp p_Result p0_Result−:=

dp0 p0_Result pa1_Result−:=dp0 p0_Result pa1_Result−:=

Calculations of Fluid Velocities at GT Manifold and Feeder Lines:

Manifold Section at tee fitting:

v_in

m°A

ρ p_Result T,( )

dT_in2

π⋅

4

:=v_in

m°A

ρ p_Result T,( )

dT_in2

π⋅

4

:=

CALCULATIONS

Calculations for Pressure Differences:

dpfeeder1 pa1_Result p1B_Result−:=dpfeeder1 pa1_Result p1B_Result−:= dpa1 pa1_Result p1_Result−:=dpa1 pa1_Result p1_Result−:=









4 4

v_out

m°

ρ p0_Result T,( )

dT_out2

π⋅

4

:=v_out

m°

ρ p0_Result T,( )

dT_out2

π⋅

4

:=

Manifold Section 0:

v0_in

m°

ρ p0_Result T,( )

d02

π⋅

4

:=v0_in

m°

ρ p0_Result T,( )

d02

π⋅

4

:=

v0_out

m°

ρ p1_Result T,( )

d02

π⋅

4

:=v0_out

m°

ρ p1_Result T,( )

d02

π⋅

4

:=

Manifold Section A:

vA_in

m° m°1_Result−( )ρ p1_Result T,( )

dA2

π⋅

4

:=vA_in


dA2

π⋅

4

:=

vA_out


dA2

π⋅

4

:=vA_out


dA2

π⋅

4

:=

Manifold Section B:

vB_in

m° m°1_Result− m°2_Result−( )ρ p2_Result T,( )

dB2

π⋅

4

:=vB_in


dB2

π⋅

4

:=

vB_out


dB2

π⋅

4

:=vB_out


dB2

π⋅

4

:=

Manifold Section C:

vC_in

m° m°1_Result− m°2_Result− m°3_Result−( )ρ p3_Result T,( )

dC2

π⋅

4

:=vC_in


dC2

π⋅

4

:=

vC_out


dC2

π⋅

4

:=vC_out


dC2

π⋅

4

:=

Manifold Section D:

vD_in

m° m°1_Result− m°2_Result− m°3_Result− m°4_Result−( )ρ p4_Result T,( )

dD2

π⋅

4

:=vD_in


dD2

π⋅

4

:=

vD_out


dD2

π⋅

4

:=vD_out


dD2

π⋅

4

:=

Manifold Section E:

vE_in

m° m°1_Result− m°2_Result− m°3_Result− m°4_Result− m°5_Result−( )ρ p5_Result T,( )

dE2

π⋅

4

:=vE_in


dE2

π⋅

4

:=



vE_out

ρ p6_Result T,( )

dE2

π⋅

4

:=vE_out

ρ p6_Result T,( )

dE2

π⋅

4

:=

Manifold Section F:

vF_in

m° m°1_Result− m°2_Result− m°3_Result− m°4_Result− m°5_Result− m°6_Result−( )ρ p6_Result T,( )

dF2

π⋅

4

:=vF_in


dF2

π⋅

4

:=

vF_out


dF2

π⋅

4

:=vF_out


dF2

π⋅

4

:=

Manifold Section G:

vG_in

m° m°1_Result− m°2_Result− m°3_Result− m°4_Result− m°5_Result− m°6_Result− m°7_Result−( )ρ p7_Result T,( )

dG2

π⋅

4

:=vG_in


dG2

π⋅

4

:=

vG_out


dG2

π⋅

4

:=vG_out


dG2

π⋅

4

:=

Feeder Line (1) - inlet: Feeder Line (1) - outlet:

v1_in

m°1_Result

ρ p1_Result T,( )

d12

π⋅

4

:=v1_in

m°1_Result

ρ p1_Result T,( )

d12

π⋅

4

:=v1_out

m°1_Result

ρ p1B_Result T,( )

d12

π⋅

4

:=v1_out

m°1_Result

ρ p1B_Result T,( )

d12

π⋅

4

:=

v6_out

m°6_Result

ρ p6B_Result T,( )

d62

π⋅

4

:=v6_out

m°6_Result

ρ p6B_Result T,( )

d62

π⋅

4

:=v6_in

m°6_Result

ρ p6_Result T,( )

d62

π⋅

4

:=v6_in

m°6_Result

ρ p6_Result T,( )

d62

π⋅

4

:=

Feeder Line (6) - outlet:Feeder Line (6) - inlet:

v5_out

m°5_Result

ρ p5B_Result T,( )

d52

π⋅

4

:=v5_out

m°5_Result

ρ p5B_Result T,( )

d52

π⋅

4

:=v5_in

m°5_Result

ρ p5_Result T,( )

d52

π⋅

4

:=v5_in

m°5_Result

ρ p5_Result T,( )

d52

π⋅

4

:=


v4_out

m°4_Result

ρ p4B_Result T,( )

d42

π⋅

4

:=v4_out

m°4_Result

ρ p4B_Result T,( )

d42

π⋅

4

:=v4_in

m°4_Result

ρ p4_Result T,( )

d42

π⋅

4

:=v4_in

m°4_Result

ρ p4_Result T,( )

d42

π⋅

4

:=


v3_out

m°3_Result

ρ p3B_Result T,( )

d32

π⋅

4

:=v3_out

m°3_Result

ρ p3B_Result T,( )

d32

π⋅

4

:=v3_in

m°3_Result

ρ p3_Result T,( )

d32

π⋅

4

:=v3_in

m°3_Result

ρ p3_Result T,( )

d32

π⋅

4

:=


v2_out

m°2_Result

ρ p2B_Result T,( )

d22

π⋅

4

:=v2_out

m°2_Result

ρ p2B_Result T,( )

d22

π⋅

4

:=v2_in

m°2_Result

ρ p2_Result T,( )

d22

π⋅

4

:=v2_in

m°2_Result

ρ p2_Result T,( )

d22

π⋅

4

:=


4 4


v7_in

m°7_Result

ρ p7_Result T,( )

d72

π⋅

4

:=v7_in

m°7_Result

ρ p7_Result T,( )

d72

π⋅

4

:=v7_out

m°7_Result

ρ p7B_Result T,( )

d72

π⋅

4

:=v7_out

m°7_Result

ρ p7B_Result T,( )

d72

π⋅

4

:=


v8_in

m°8_Result

ρ p8_Result T,( )

d82

π⋅

4

:=v8_in

m°8_Result

ρ p8_Result T,( )

d82

π⋅

4

:= v8_out

m°8_Result

ρ p8B_Result T,( )

d82

π⋅

4

:=v8_out

m°8_Result

ρ p8B_Result T,( )

d82

π⋅

4

:=

ρ p3_Result T,( ) =p3_Resultp4_Result bar=p4_ResultdpC bar=dpCp3_Result bar=p3_Result

ρ p2_Result T,( ) =p2_Resultp3_Result bar=p3_ResultdpB bar=dpBp2_Result bar=p2_Result

ρ p1_Result T,( ) =p1_Resultp2_Result bar=p2_ResultdpA bar=dpAp1_Result bar=p1_Result

ρ p0_Result T,( ) =p0_Resultp1_Result bar=p1_Resultdp0 bar=dp0p0_Result bar=p0_Result

ρ p_Result T,( ) =p_Result

ρ p7_Result T,( ) =p7_Resultp8_Result bar=p8_ResultdpG bar=dpG

p7_Result bar=p7_Result

ρ p6_Result T,( ) =p6_Result

p7_Result bar=p7_ResultdpF bar=dpFp6_Result bar=p6_Result

ρ p5_Result T,( ) =p5_Result

p6_Result bar=p6_ResultdpE bar=dpEp5_Result bar=p5_Result

ρ p4_Result T,( ) =p4_Resultp5_Result bar=p5_ResultdpD bar=dpD

p4_Result bar=p4_Result

λ6_Result =λ6_Result

λ5_Result =λ5_Resultλ4_Result =λ4_Resultλ3_Result =λ3_Resultλ2_Result =λ2_Resultλ1_Result =λ1_Result

λG_Result =λG_ResultλF_Result =λF_Result

λE_Result =λE_ResultλD_Result =λD_ResultλC_Result =λC_ResultλB_Result =λB_ResultλA_Result =λA_Resultλ0_Result =λ0_Result

Results for Lambda:

RESULTS

p0_Result bar=p0_Resultdp bar=dpp_Result bar=p_Result

Manifold: Results for Pressures, Pressure Losses and associated Fuel Gas Densities:

m°8_Result =m°8_Resultm°7_Result =m°7_Resultm°6_Result =m°6_Resultm°5_Result =m°5_Result

m°4_Result =m°4_Resultm°3_Result =m°3_Resultm°2_Result =m°2_Resultm°1_Result =m°1_Result

m° 4.81kg

s=m°A 9.62

kg

s=

Results for Mass Balance:

λ8_Result =λ8_Resultλ7_Result =λ7_Result

p5_Result bar=p5_Result dp5 bar=dp5 p52 20 bar=ρ p5_Result T,( ) =p5_Result

pa5_Result bar=pa5_Result dpfeeder5 bar=dpfeeder5







Feeder Lines: Results for Pressures, Pressure Losses and associated Fuel Gas Densities:









pcc 20 bar=

Condition_5B =Condition_5B

p5B_Result bar=p5B_Result ρ p5B_Result T,( ) =p5B_Resultdp5B bar=dp5B pcc 20 bar=







Burners: Results for Burner Pressure Losses:








p4B_Result bar=p4B_Result ρ p4B_Result T,( ) =p4B_Resultdp4B bar=dp4B

vG_out =vG_outvG_in =vG_in

Manifold Section G:

vF_out =vF_outvF_in =vF_in

Manifold Section F:

vE_out =vE_outvE_in =vE_in

Manifold Section E:

vD_out =vD_outvD_in =vD_in

Manifold Section D:

vC_out =vC_outvC_in =vC_in

Manifold Section C:

vB_out =vB_outvB_in =vB_in

Manifold Section B:

vA_out =vA_outvA_in =vA_in

Manifold Section A:

v0_out =v0_outv0_in =v0_in

Manifold Section 0:

v_out =v_outv_in =v_in

Manifold Section at tee fitting:

Manifold: Results for Velocities:


Feeder Line (8):


Feeder Line (7):


Feeder Line (6):


Feeder Line (5):


Feeder Line (4):


Feeder Line (3):


Feeder Line (2):


Feeder Line (1):

Feeder Lines: Results for Velocities:

η 488 K⋅( ) 1.759 105−

×kg

m s=

η T( )

0.72kg

m3

⋅

2.444 105−

×m

2

s=

κ 1.315=

m° 4.81kg

s= m°A 9.62

kg

s=

m°

120.401

kg

s=

m°1, m°2, m°3, m°4, m°5, m°6, m°7, m°8, m°9, m°10, m°11, m°12, pa1, pa2, pa3, pa4, pa5, pa6, pa7, pa8, pa9, pa10, pa11, pa12, p1, ,

dpfeeder1 bar=dpfeeder1 dpa1 bar=dpa1



dpa4 bar=dpa4dpfeeder4 bar=dpfeeder4

dpa5 bar=dpa5dpfeeder5 bar=dpfeeder5

dpa6 bar=dpa6



dpfeeder8 bar=dpfeeder8

m°1_Result m°2_Result+ m°3_Result+ m°4_Result+ m°5_Result+ m°6_Result+ m°7_Result+ m°8_Result+ =m°1_Result

m° 4.81kg

s=

Total ammount of mass flow m°

Verification of mass balance for m°:

m°8 0.401kg

s=m°7 0.401

kg

s=m°6 0.401

kg

s=m°5 0.401

kg

s=

m°4 0.401kg

s=m°3 0.401

kg

s=m°2 0.401

kg

s=m°1 0.401

kg

s=

λ7 0.015=λ6 0.015=λ5 0.015=λ4 0.015=λ3 0.015=λ2 0.015=λ1 0.015=

λG 0.015=λF 0.015=λE 0.015=λD 0.015=λC 0.015=λB 0.015=λA 0.015=λ0 0.015=

Schätzwerte für Iteration:

Verification of calculated pressure p0 at manifold inlet:

Required pressure p at GT Manifold Piping Inlet

p_Result bar=p_Result

pcc dp1B+ dp1+ dpa1+ dp0+ dp+ bar=dp1B

pcc dp2B+ dp2+ dpa2+ dpA+ dp0+ dp+ bar=dp2B

pcc dp3B+ dp3+ dpa3+ dpB+ dpA+ dp0+ dp+ bar=dp3B

pcc dp4B+ dp4+ dpa4+ dpC+ dpB+ dpA+ dp0+ dp+ bar=dp4B

pcc dp5B+ dp5+ dpa5+ dpD+ dpC+ dpB+ dpA+ dp0+ dp+ bar=dp5B

pcc dp6B+ dp6+ dpa6+ dpE+ dpD+ dpC+ dpB+ dpA+ dp0+ dp+ bar=dp6B

pcc dp7B+ dp7+ dpa7+ dpF+ dpE+ dpD+ dpC+ dpB+ dpA+ dp0+ dp+ bar=dp7B

pcc dp8B+ dp8+ dpa8+ dpG+ dpF+ dpE+ dpD+ dpC+ dpB+ dpA+ dp0+ dp+ bar=dp8B

definition of units -...

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