Femi Trial

8/10/2019 Femi Trial

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Aspen Flare System Analyzer V8.0 - aspenONE

Version 27.0.0.35

User Name : OLUFEMI

Job Code :

Project :

Description :

Network

Name Location Upstream

Node

Downstream

Node

Ignored Tailpipe Length

(m)

FLARE STACK Connector1 FLARE TIP No Yes 20.000

FLARE HEADER Tee1 Connector1 No No 100.000

Pipe1 ReliefValve1 Tee1 No Yes 0.000

Pipe2 ControlValve1 Tee1 No No 20.000

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Description :

Network

Name Elevation

Change(m)

Material Roughness

(mm)

Thermal

Conductivity(W/m-K)

Nominal

Diameter

Sc hedul e Internal

Diameter(mm)

Wall

Thickness(mm)

FLARE STACK 20.000 Stainless Steel 0.02540 16.29 16inch 5S 398.018 4.191

FLARE HEADER 0.000 Carbon Steel 0.04572 51.91 16inch 40 381.000 12.700

Pipe1 0.000 Carbon Steel 0.04572 51.91 16inch 40 381.000 12.700

Pipe2 0.000 Carbon Steel 0.04572 51.91 16inch 40 381.000 12.700


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Description :

Network

Name Pipe

Class

Sizeable Length

Multiplier

Fittings

Loss A

Fittings

Loss B

Ambient

Temperature(C)

External Medium

Velocity(m/s)

Insulation

Description

Insulation

Thickness(mm)

FLARE STACK No Yes 0.000 0.000 Glass Fibre 0.00

FLARE HEADER No Yes 0.000 0.000 Glass Fibre 0.00

Pipe1 No Yes 0.000 0.000 Glass Fibre 0.00

Pipe2 No Yes 0.000 0.000 Glass Fibre 0.00


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Description :

Network

Name Insulation

Conductivity(W/m-K)

Outlet

Temperature(C)

Duty

(kJ/hr)

VLE

Method

Horizontal

Pres. Drop

Inclined

Pres. Drop

FLARE STACK 0.040 0.000e+000 Peng Robinson Beggs and Brill HomogBeggs and Brill Homog

FLARE HEADER 0.040 0.000e+000 Peng Robinson Beggs and Brill HomogBeggs and Brill Homog

Pipe1 0.040 0.000e+000 Model Default Model Default Model Default

Pipe2 0.040 0.000e+000 Peng Robinson Beggs and Brill HomogBeggs and Brill Homog

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Version 27.0.0.35

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Job Code :

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Description :

Network

Name Vertical

Pres. Drop

Two Phase

Elements

Friction

Factor

Damping

Factor

FLARE STACK Beggs and Brill Homog Model Default

FLARE HEADER Beggs and Brill Homog Model Default

Pipe1 Model Default Model Default

Pipe2 Beggs and Brill Homog Model Default


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Version 27.0.0.35

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Description :

Node Data

Name Location Ignored Node

Type

Connections

FLARE TIP No Flare Tip Inlet: FLARE STACK

Connector1 No Connector Upstream: FLARE HEADERDownstream: FLARE STACK

Tee1 No Tee Upstream: Pipe1Branch: Pipe2Downstream: FLARE HEADER

ReliefValve1 No Relief Valve Outlet: Pipe1

ControlValve1 No Control Valve Outlet: Pipe2


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Version 27.0.0.35

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Description :

Node Data

Name Calculations

FLARE TIP User Pressure Drop Curve UsedDiameter =300.000 : Two Phase Correction =NoIncompressible Calculation =Compressible : Compressible Transition = : Isothermal Pressure Drop =Yes

Connector1 Fittings Loss Method =Calculated : Two Phase Correction =YesIncompressible Calculation =Incompressible (Crane): Compressible Transition =10.0%: Isothermal Pressure Drop =YeTheta =90.00 deg

Tee1 Fittings Loss Method =Miller : Two Phase Correction =YesIncompressible Calculation =Incompressible (Crane): Compressible Transition =10.0%: Isothermal Pressure Drop =YeTheta =90 deg : Body=Tail

ReliefValve1 MAWP =10.00000 bar : Flange Diameter = : Number Of Valves =1 : Orifice Area Per Valve =7129.032 mm2Valve Type =Balanced : Fittings Loss Method = : Two Phase Correction =YesIncompressible Calculation =Incompressible (Crane): Compressible Transition =10.0%: Isothermal Pressure Drop =Ye

ControlValve1 Fittings Loss Method =Calculated : Two Phase Correction =YesIncompressible Calculation =Incompressible (Crane): Compressible Transition =10.0%: Isothermal Pressure Drop =Ye


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Description :

Component Data

Name ID Mol. Wt. Critical

Temperature(K)

Critical

Pressure(bar)

Critical

Volume(m3/kgmole)

Char.

Volume(m3/kgmole)

Accentr ic

Factor

SRK Accent

Factor

Methane 16.043 190.70 46.407 0.09900 0.09939 0.01150 0.00740

Ethane 30.070 305.43 48.839 0.14800 0.14575 0.09860 0.09830

Propane 44.097 369.90 42.567 0.20000 0.20008 0.15240 0.15320


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Description :

Component Data

Name Norm. Boiling

Point(K)

Standard

Density(kg/m3)

Watson

Factor

Enthalpy

Term A(kJ/kgmole)

Enthalpy

Term B(kJ/kgmole/K)

Enthalpy

Term C(kJ/kgmole/K^2)

Enthalpy

Term D(kJ/kgmole/K^3)

Methane 111.63 299.39 19.563 -2.08237e+002 3.79349e+001 -3.42110e-002 9.08317e-005

Ethane 184.55 355.68 19.471 -5.31486e+001 3.43669e+001 -9.73062e-003 1.27590e-004

Propane 231.05 506.68 14.732 1.74134e+003 1.74183e+001 9.32250e-002 1.74838e-005


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Component Data

Name Enthalpy

Term E(kJ/kgmole/K^4)

Enthalpy

Term F(kJ/kgmole/K^5)

Entropy

Term

Viscosity

A Term

Viscosity

B Term

Type

Methane -5.97560e-008 1.38113e-011 1.00000e+000 -0.00201 0.02547 HC

Ethane -1.02032e-007 2.65245e-011 1.00000e+000 0.07231 0.04698 HC

Propane -2.94205e-008 7.40547e-012 1.00000e+000 0.07112 -0.06538 HC


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Description :

Scenario Data

Name Tailpipe

Rho V2(kg/m/s2)

Tailpipe

Noise(dB)

Default Scenario 100.0

Scenario1 100.0

Scenario2 100.0

Scenario3 100.0


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Description :

Fittings

Name Location Upstream

Node

Downstream

Node

Fitting List


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Description :

Messages:Basis

No. Message

1 Ambient temperature =15.00 C

2 Atmospheric pressure =1.01325 bar

3 Checkfor choke flow =False

4 Enable heat transfer calculations =False

5 External radiation =False

6 Calculation mode =Rating

7 Rated flow =False

8 Rated flow nodes =False

9 Rated flow tailpipe =False

10 External medium velocity=10.00 m/s

11 Include kinetic energy=False

12 Ignore kinetic energyin separators =False

13 Code for kinetic energybasis =Inlet Pipe Velocity14 Calculate ignored sources as zero flow =False

15 CheckMABP for inactive sources =False

16 Ignore valve flange size change in design calculations =True

17 Maximum system velocity=500.000 m/s

18 Code to indicate which scenarios are calculated =All Scenarios

19 VLE =Compressible Gas

20 Code for enthalpymethod =Ideal Gas

21 Vle source outlet temperature =Peng Robinson

22 Enthalpysource outlet temperature =Peng Robinson

23 Code for horizontal pressure drop method =Isothermal Gas

24 Code for inclined pressure drop method =Isothermal Gas

25 Code for vertical pressure drop method =Isothermal Gas

26 Number of elements for pipe calculation =10

27 Friction factor =Chen28 Use pipe roughness for fitting or not?=Yes

29 Roughness for fitting =0.04572 mm

30 Warn mach number for sizing =True

31 Warn velocityfor sizing =True

32 Warn Rho V2 for sizing =True

33 Warn noise for sizing =True

34 Warn ice form for sizing =True

35 Warn BP for sizing =True

36 Warn choke for sizing =True

37 Warn slug for sizing =True

38 Warn temperature for sizing =True

39 Warn pressure basis =Static Pressure

40 Warn physical propertyfailure =True

41 Warn heat balance failure =True42 Warn choke pressure failure =True

43 Warn pressure drop failure =True

44 Warn liquid with vapour method failure =True

45 Warn Correlation range failure =True

46 Warn initial while sizing =True

47 Warn size change while sizing =True

48 Warn limit reached while sizing =True


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Version 27.0.0.35

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Description :

Messages:Basis

No. Message

49 Pressure tolerance in properties loop (%)=1.0e-004

50 Pressure tolerance for unit operation calculations (%)=1.0e-003

51 Pressure tolerance for loop calculations (%)=1.0e-002

52 Mass balance tolerance in outer loop (%)=1.0e+000

53 Number of iterations in inner (properties)loop =25

54 Number of iterations for loop calculations =500

55 Damping factor for inner (properties)loop =1.0e+000

56 Damping factor for loop calculations =1.0e+000

57 Select loop convergence method =Newton Raphson

58 Select analyzer for looped systems =Convergent

59 Are loop calculations echoed =False

60 Keep bad =False

61 Update flow estimates from solution =Do Not Update62 Initial pressure for propertycalculations =1.01325 bar

63 Multiplier for pipe length =1.00

64 Initial phase method for sizing =Multi Phase

65 Minimum temperature for carbon steel =-29.00 C

66 Maximum temperature for carbon steel =400.00 C

67 Minimum temperature for stainless steel =-69.20 C

68 Maximum temperature for stainless steel =500.00 C

69 Inlet flow check=

70 Gauge inlet check=False

71 Ignore inlet =

72 Design option =False

73 Design schedule =40

74 Engine =Flarenet Solver Engine


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Description :

Messages:Sizer

No. Message


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Description :

Messages:Loop

No. Message


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Description :

Scenario : Default Scenario

Source Data

Name Location Outlet

Pipe

Type Ignored Inlet

Pressure(bar)

Inlet Temp.

Spec.(C)

ReliefValve1 Pipe1 Relief Valve No 10.89868 25.00

ControlValve1 Pipe2 Control Valve No 10.00000 25.00


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Version 27.0.0.35

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Description :


Source Data

Name Allowable

Backpressure(bar)

Outlet

Temperature(C)

Mass

Flow(kg/hr)

Rated Mass

Flow(kg/hr)

Outlet Flange

Diameter(mm)

Valv es Reli efValve

Type

Ori fice

Area(mm2)

ReliefValve1 4.60795 25.00 0.0 56071.0 1 Balanced 7129.032

ControlValve1 5.00000 25.00 2935.0


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Description :


Source Data

Name Orifi ce B ac k Pres.

Limit(bar)

Outlet Fittings

Loss Method

Inlet Length

(m)

Inlet Elev.

Change(m)

Inlet Material Inlet Roughness

(mm)

Inlet Nom.

Diameter

ReliefValve1 api_Q Calculated 0.0000 0.0000 Carbon Steel 0.04572 12 inch

ControlValve1 Calculated 0.00 0.00 Carbon Steel 0.04572 12 inch


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Description :


Source Data

Name Inlet

Schedule

Inlet Intern.

Diameter(mm)

Inlet Pipe

Class

Inlet Fittings

Loss A

Inlet Fittings

Loss B

Static Inlet

Pres. Drop(bar)

VLE

Method

Inlet Temp.

Calc.(C)

Vapour

Fraction

ReliefValve1 40 303.2252 No 0.000 0.000 Peng Robinson 25.00 1.000000

ControlValve1 40 303.225 No 0.000 0.000 Peng Robinson 25.00 1.000000


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Description :


Source Data

Name Enthalpy

(kJ/hr)

Entropy

(kJ/kgmole/K)

Energy

(kJ/hr)

Composition

Basis

Mol. Wt. Methane Ethane

ReliefValve1 11956.51 233.947 0.000e+000 Molecular Weight 30.0000 0.004983 0.995017

ControlValve1 11956.51 233.947 1.170e+006 Molecular Weight 30.0000 0.004983 0.995017


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Pressure/Flow Summary(Veloci ties Based Upon Nominal Flows)

Name Mass

Flow(kg/hr)

Molar

Flow(kgmole/hr)

Rated Mass

Flow(kg/hr)

Static Pressure

Drop(bar)

Noise

(dB)

Static Source

Back Pressure(bar)

FLARE STACK 2935.0 97.83 59006.0 0.00256 1.1

FLARE HEADER 2935.0 97.83 59006.0 0.00085 0.0

Pipe1 0.0 0.00 56071.0 0.00000 0.0 1.01695

Pipe2 2935.0 97.83 2935.0 0.00017 0.0 1.01704


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Name Upstream

Static Pressure(bar)

Upstream

Temperature(C)

Upstream

Velocity(m/s)

Upstream

Mach No.

Upstream

Rho V2(kg/m/s2)

Upstream

Enthalpy Flow(kJ/hr)

FLARE STACK 1.01581 24.99 5.285 0.017 35 1.170e+006

FLARE HEADER 1.01664 24.99 5.763 0.018 41 1.170e+006

Pipe1 1.01695 24.99 0.000 0.000 0 1.196e-004

Pipe2 1.01704 24.99 5.761 0.018 41 1.170e+006


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Name Downstream


Downstream

Temperature(C)

Downstream

Velocity(m/s)

Downstream

Mach No.

Downstream

Rho V2(kg/m/s2)

Downstream


FLARE STACK 1.01325 25.00 5.299 0.017 35 1.170e+006

FLARE HEADER 1.01578 25.00 5.768 0.018 41 1.170e+006

Pipe1 1.01695 25.00 0.000 0.000 0 1.196e-004

Pipe2 1.01686 25.00 5.762 0.018 41 1.170e+006


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Description :



Name Flow

Regime

Static Pipe

Friction Loss(bar)

Static Pipe

Accel. Loss(bar)

Static Pipe

Elevation Loss(bar)

Static Pipe

Fittings Loss(bar)

Friction

Factor

FLARE STACK Single Phase/Single Phase 0.00013 0.00000 0.00243 0.00000 0.01538

FLARE HEADER Single Phase/Single Phase 0.00085 0.00000 0.00000 0.00000 0.01577

Pipe1 Single Phase/Single Phase 0.00000 0.00000 0.00000 0.00000 0.00000



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Name Reynolds

Number

Duty

(kJ/hr)

Overall

HTC(W/m2/C)

External

Convective HTC(W/m2/C)

External

Radiative HTC(W/m2/C)

Internal

HTC(W/m2/C)

FLARE STACK 272354 0.000e+000

FLARE HEADER 284518 0.000e+000

Pipe1 0 0.000e+000

Pipe2 284518 0.000e+000


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Name Wall

Temperature(C)

External

Temperature(C)

Equivalent

Length(m)

Physical

Length(m)

FLARE STACK 20.00 20.000

FLARE HEADER 100.00 100.000

Pipe1 0.00 0.000

Pipe2 20.00 20.000


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Description :

Scenario : Scenario1

Source Data


Pipe

Type Ignored Inlet

Pressure(bar)

Inlet Temp.

Spec.(C)




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Source Data

Name Allowable

Backpressure(bar)

Outlet

Temperature(C)

Mass

Flow(kg/hr)

Rated Mass

Flow(kg/hr)

Outlet Flange

Diameter(mm)


Type

Ori fice

Area(mm2)


ControlValve1 5.00000 25.00 0.0


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Description :


Source Data


Limit(bar)

Outlet Fittings

Loss Method

Inlet Length

(m)

Inlet Elev.

Change(m)


(mm)

Inlet Nom.

Diameter




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Source Data

Name Inlet

Schedule

Inlet Intern.

Diameter(mm)

Inlet Pipe

Class

Inlet Fittings

Loss A

Inlet Fittings

Loss B

Static Inlet

Pres. Drop(bar)

VLE

Method

Inlet Temp.

Calc.(C)

Vapour

Fraction




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Source Data

Name Enthalpy

(kJ/hr)

Entropy

(kJ/kgmole/K)

Energy

(kJ/hr)

Composition

Basis





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Name Mass

Flow(kg/hr)

Molar

Flow(kgmole/hr)

Rated Mass

Flow(kg/hr)

Static Pressure

Drop(bar)

Noise

(dB)

Static Source

Back Pressure(bar)

FLARE STACK 2935.0 97.83 56071.0 0.00256 1.1

FLARE HEADER 2935.0 97.83 56071.0 0.00085 0.0

Pipe1 2935.0 97.83 56071.0 0.00000 0.0 1.01668

Pipe2 0.0 0.00 0.0 0.00000 0.0 1.01672


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Name Upstream


Upstream

Temperature(C)

Upstream

Velocity(m/s)

Upstream

Mach No.

Upstream

Rho V2(kg/m/s2)

Upstream


FLARE STACK 1.01581 24.99 5.285 0.017 35 1.170e+006

FLARE HEADER 1.01664 24.99 5.763 0.018 41 1.170e+006

Pipe1 1.01668 24.99 5.763 0.018 41 1.170e+006

Pipe2 1.01672 24.99 0.000 0.000 0 1.196e-004


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Name Downstream


Downstream

Temperature(C)

Downstream

Velocity(m/s)

Downstream

Mach No.

Downstream

Rho V2(kg/m/s2)

Downstream


FLARE STACK 1.01325 25.00 5.299 0.017 35 1.170e+006

FLARE HEADER 1.01578 25.00 5.768 0.018 41 1.170e+006

Pipe1 1.01668 25.00 5.766 0.018 41 1.170e+006

Pipe2 1.01672 25.00 0.000 0.000 0 1.196e-004


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Name Flow

Regime

Static Pipe

Friction Loss(bar)

Static Pipe

Accel. Loss(bar)

Static Pipe

Elevation Loss(bar)

Static Pipe

Fittings Loss(bar)

Friction

Factor



Pipe1 Single Phase/Single Phase 0.00000 0.00000 0.00000 0.00000



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Name Reynolds

Number

Duty

(kJ/hr)

Overall

HTC(W/m2/C)

External


External


Internal

HTC(W/m2/C)

FLARE STACK 272354 0.000e+000


Pipe1 284518 0.000e+000

Pipe2 0 0.000e+000


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Name Wall

Temperature(C)

External

Temperature(C)

Equivalent

Length(m)

Physical

Length(m)



Pipe1 0.00 0.000

Pipe2 20.00 20.000


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Source Data

Name Allowable

Backpressure(bar)

Outlet

Temperature(C)

Mass

Flow(kg/hr)

Rated Mass

Flow(kg/hr)

Outlet Flange

Diameter(mm)


Type

Ori fice

Area(mm2)


ControlValve1 5.00000 25.00 0.0


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Source Data

Name Inlet

Schedule

Inlet Intern.

Diameter(mm)

Inlet Pipe

Class

Inlet Fittings

Loss A

Inlet Fittings

Loss B

Static Inlet

Pres. Drop(bar)

VLE

Method

Inlet Temp.

Calc.(C)

Vapour

Fraction




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Source Data

Name Enthalpy

(kJ/hr)

Entropy

(kJ/kgmole/K)

Energy

(kJ/hr)

Composition

Basis





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Name Mass

Flow(kg/hr)

Molar

Flow(kgmole/hr)

Rated Mass

Flow(kg/hr)

Static Pressure

Drop(bar)

Noise

(dB)

Static Source

Back Pressure(bar)

FLARE STACK 2935.0 97.83 56071.0 0.00256 1.1

FLARE HEADER 2935.0 97.83 56071.0 0.00085 0.0

Pipe1 2935.0 97.83 56071.0 0.00000 0.0 1.01668

Pipe2 0.0 0.00 0.0 0.00000 0.0 1.01672


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Name Upstream


Upstream

Temperature(C)

Upstream

Velocity(m/s)

Upstream

Mach No.

Upstream

Rho V2(kg/m/s2)

Upstream


FLARE STACK 1.01581 24.99 5.285 0.017 35 1.170e+006

FLARE HEADER 1.01664 24.99 5.763 0.018 41 1.170e+006

Pipe1 1.01668 24.99 5.763 0.018 41 1.170e+006

Pipe2 1.01672 24.99 0.000 0.000 0 1.196e-004


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Name Downstream


Downstream

Temperature(C)

Downstream

Velocity(m/s)

Downstream

Mach No.

Downstream

Rho V2(kg/m/s2)

Downstream


FLARE STACK 1.01325 25.00 5.299 0.017 35 1.170e+006

FLARE HEADER 1.01578 25.00 5.768 0.018 41 1.170e+006

Pipe1 1.01668 25.00 5.766 0.018 41 1.170e+006

Pipe2 1.01672 25.00 0.000 0.000 0 1.196e-004


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Name Flow

Regime

Static Pipe

Friction Loss(bar)

Static Pipe

Accel. Loss(bar)

Static Pipe

Elevation Loss(bar)

Static Pipe

Fittings Loss(bar)

Friction

Factor






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Name Reynolds

Number

Duty

(kJ/hr)

Overall

HTC(W/m2/C)

External


External


Internal

HTC(W/m2/C)

FLARE STACK 272354 0.000e+000


Pipe1 284518 0.000e+000

Pipe2 0 0.000e+000


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Name Wall

Temperature(C)

External

Temperature(C)

Equivalent

Length(m)

Physical

Length(m)



Pipe1 0.00 0.000

Pipe2 20.00 20.000


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Source Data


Pipe

Type Ignored Inlet

Pressure(bar)

Inlet Temp.

Spec.(C)




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Source Data

Name Allowable

Backpressure(bar)

Outlet

Temperature(C)

Mass

Flow(kg/hr)

Rated Mass

Flow(kg/hr)

Outlet Flange

Diameter(mm)


Type

Ori fice

Area(mm2)


ControlValve1 5.00000 25.00 0.0


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Source Data


Limit(bar)

Outlet Fittings

Loss Method

Inlet Length

(m)

Inlet Elev.

Change(m)


(mm)

Inlet Nom.

Diameter




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Source Data

Name Inlet

Schedule

Inlet Intern.

Diameter(mm)

Inlet Pipe

Class

Inlet Fittings

Loss A

Inlet Fittings

Loss B

Static Inlet

Pres. Drop(bar)

VLE

Method

Inlet Temp.

Calc.(C)

Vapour

Fraction




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Source Data

Name Enthalpy

(kJ/hr)

Entropy

(kJ/kgmole/K)

Energy

(kJ/hr)

Composition

Basis





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Name Mass

Flow(kg/hr)

Molar

Flow(kgmole/hr)

Rated Mass

Flow(kg/hr)

Static Pressure

Drop(bar)

Noise

(dB)

Static Source

Back Pressure(bar)

FLARE STACK 2000.0 66.67 56071.0 0.00249 0.0

FLARE HEADER 2000.0 66.67 56071.0 0.00042 0.0

Pipe1 2000.0 66.67 56071.0 0.00000 0.0 1.01617

Pipe2 0.0 0.00 0.0 0.00000 0.0 1.01619


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Name Upstream


Upstream

Temperature(C)

Upstream

Velocity(m/s)

Upstream

Mach No.

Upstream

Rho V2(kg/m/s2)

Upstream


FLARE STACK 1.01574 24.99 3.602 0.012 16 7.971e+005

FLARE HEADER 1.01615 24.99 3.929 0.013 19 7.971e+005

Pipe1 1.01617 24.99 3.929 0.013 19 7.971e+005

Pipe2 1.01619 24.99 0.000 0.000 0 1.196e-004


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Name Downstream


Downstream

Temperature(C)

Downstream

Velocity(m/s)

Downstream

Mach No.

Downstream

Rho V2(kg/m/s2)

Downstream


FLARE STACK 1.01325 25.00 3.611 0.012 16 7.971e+005

FLARE HEADER 1.01573 25.00 3.931 0.013 19 7.971e+005

Pipe1 1.01617 25.00 3.931 0.013 19 7.971e+005

Pipe2 1.01619 25.00 0.000 0.000 0 1.196e-004


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Name Flow

Regime

Static Pipe

Friction Loss(bar)

Static Pipe

Accel. Loss(bar)

Static Pipe

Elevation Loss(bar)

Static Pipe

Fittings Loss(bar)

Friction

Factor






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Name Reynolds

Number

Duty

(kJ/hr)

Overall

HTC(W/m2/C)

External


External


Internal

HTC(W/m2/C)

FLARE STACK 185590 0.000e+000


Pipe1 193880 0.000e+000

Pipe2 0 0.000e+000


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Name Wall

Temperature(C)

External

Temperature(C)

Equivalent

Length(m)

Physical

Length(m)



Pipe1 0.00 0.000

Pipe2 20.00 20.000

Documents

Femi Trial