Task Agung Prabowo.xlsx

DANI SASMITRA

Pipa 18" In Pipe OD ID L At P1 Q Jenis Pipe Densitas Viskositas T Velocity Nre

1507113627

Q = 500 m^3/h 20 in 20 in 19.25 in 1181.1 in 291 in2 3.8 kg/cm^2 8475.52008 in^3/s Carbon Steel

30 C 2.4271741998 ft/s 450179.762441117 Turbulen

Friction Loss pada Pipa 18" dan 1,5" 1. Friction loss in 18 in straight pipe 2. Contraction loss from 18 in pipe to 1,5 in pipe 3. Friction loss in 1,5 in straight pipe 4. Friction in 1,5 inc 4 elbow

0.508001016 m 0.508001016 m 0.488950978 m 30 m 0.187742311 m2 3.726527 bar 0.138888889 m^3/s

1.66665 1.66665 1.60415 98.424 2.020792 54.04854 4.904815

995.68000 kg/m3 0.80000 cp 303 K

62.15831 0.000538

1). Friction loss in 18 in straight pipe L e e/D f Ff

30 m 0.000046 m 0.000094079 0.006 0.1348153406 lbf ft/lbm

98.4252 ft 0.000151 ft

30 m 0.000046 m 0.0011248571 0.0055 12.0265550794 lbf ft/lbm

98.4252 ft 0.000151 ft

2. Contraction loss from 18 in pipe to 1,5 in pipe Kc 0.5461443299 hc 0.4069676651 ft.lbf/lbm 3. Friction loss in 1,5 in straight pipe Asumsi L e e/D f Ff

4. Friction in 1,5 inc 4 elbow hf 2.2354951402 ft.lbf/lbm

Total Friksi 14.8038332253 ft.lbf/lbm

ft ft ft ft ft2 psi ft^3/s lb/ft3 lbm/ft s

2173.913 gpm 74534.13 bpd

Pipa 1,5'' In Pipe OD ID L At P1 Q Jenis Pipe Densitas Viskositas T Velocity Nre

1.5 in 1.9 in 1.61 in 1181.1 in 2.04 in2 3.8 kg/cm^2 169.5104016 in^3/s Carbon Steel

30 C 6.9245852169 ft/s 107417.22459959 Turbulen

Friction Loss pada Pipa 1,5" dan 2" 1.Friction loss in 1,5 in straight pipe 2. Friction in 1,5 inc 4 elbow 3. Contraction loss from 1,5' pipe to 2' pipe

4. Friction loss in 2' straight pipe 1. Friction loss in 1,5 in straight pipe Asumsi L e e/D f Ff

30 0.000046 0.0011248571 0.0055 12.026555079

2. Friction in 1,5 inc 4 elbow hf 2.2354951402 ft.lbf/lbm 3. Contraction loss from 1,5' pipe to 2' pipe kc 0.2150746269 hc 0.0594309092 4. Friction loss in 2' straight pipe L e e/D f Ff

2300 0.000046 0.0011248571 0.0045 217.89826407

Total Friksi 232.2197452002 ft.lbf/lbm

0.2984181395

380000 197021.2169 182978.7831

3200 5043.5561574803

0.0381001 m 0.0482601 m 0.0408941 m 30 m 0.0013161 m2 3.726527 bar 0.0027778 m^3/s

0.124999 ft 0.158332 ft 0.134165 ft 98.424 ft 0.014166 ft2 54.04854 psi 0.098096 ft^3/s

995.68000 kg/m3 0.80000 cp 303 K

62.15831 lb/ft3 0.000538 lbm/ft s

10 m^3/h

Pipa 2" In Pipe OD ID L At P1 Q Jenis Pipe Densitas Viskositas T Velocity Nre Flowrate

2 2.38 2.067 90551 3.35 3.8 169.5104016 Carbon Steel

30 4.2167623411 83979.616691311 0.0980962972 0.0027777778 10

m m

PADA PIPA 1,5 INCH SCH. NUMBER 40 DIKETAHUI N DILAKUKAN PERCOBAAN VARIASI DEBIT Q UNTUK Q ( m3/h) V (ft/s) 200 138.5 100 69.24 50 34 20 13.8 10 7

98.4252 ft 0.000151 ft

lbf ft/lbm

m m

7545.932 ft 0.000151 ft

lbf ft/lbm

0.280014 Btu/lb

Btu/lb

540143.1 J/kg

651.3127 J/kg

in in in in in2 kg/cm^2 in^3/s

C ft/s Turbulen ft^3/s m^3/s m^3/h

0.0508001016 m 0.0604521209 m 0.052501905 m 2300 m 0.0021612946 m2 3.726527 bar 0.0027777778 m^3/s 995.68000 kg/m3 0.80000 cp 303 K

0.166665 ft 0.198331 ft 0.172248 ft 7545.84 ft 0.023263 ft2 54.04854 psi 0.098096 ft^3/s 62.15831 lb/ft3 0.000538 lbm/ft s

NUMBER 40 DIKETAHUI NILAI VELOCITY MINIMUM DAN NILAI VELOCITY MAKSIMUM YANG DIPERBOLEH YAITU DIANTARA 0,6-10 FT/S VARIASI DEBIT Q UNTUK MEMPEROLEH NILAI FLOW VELOCITY YANG SESUAI SEBAGAI BERIKUT

U DIANTARA 0,6-10 FT/S

Latihan Hydraulic Calculation FEB, 8 2019 By: AGUNG PRABOWO(1507121393) Teknik Kimia UNRI 2015 Flow Available @ Point 2? Pressure Gauge = = Initial Flow =

3.8 6 0.0016666667

kg/cm2 m3/h m3/s

Pipe 1,5" Pipe 2" Elbow 90

Length (m) 30 1000 -

Diameter (m) 0.0408940818 0.052501905

Sum 1 1 4

Pipe 1,5" A v Re e e/D f dPf

= = = = = = =

0.0013161317 1.2663373366 58186.18271279 0.000046 0.0011248571 0.006 43876.88681208

m2 m/s

Elbow Kf hf dPf

= = =

0.75 0.0747627082 7476.270824597

Pipe 2" A v Re e e/D f dPf

= = = = = = =

0.0021612946 0.7711427363 45490.407513 0.000046 0.0008761587 0.0045 316834.1124491

Final Condition dPf total P Final

= =

368187.2700857 Pa 11812.72991426 Pa 0.1181272991 Kg/cm2

m

380000

Pa

(Literatur) ( Geankoplis hal 88)

Pa

J/kg Pa

m2 m/s m

(Literatur) (Dari Geankoplis hal 88)

Pa

Densitas Viskositas

= =

1000 0.00089

kg/cm3 (Literatur) Pa.s (Literatur)

CONTROL VALVE FEBRUARY, 15-2019 DESIGN AND AVAILABLE DATA Design Pressure Design Temperature TANK 1 PRESSURE TEMPERATURE H.L Hs Hf Diameter

Delta P Suction Diameter

FT DP Delta P Discharge TANK 2 Pressure high FLUID PROPERTIES Sp.Gr Viscosity FLOW RATE

AGUNG PRABOWO 1507121393 UNIVERSITAS RIAU 3.8 kg/cm2.g (maximum) 70 C

2 kg/cm2.g 38 C 1m 5m 1m 4 Inch 10.16 cm 0.1016 m 0.1 kg/cm2.g 3 Inch 7.62 cm 0.0762 m 0.2 kg/cm2.g 1.9 kg/cm2.g

Design Pressure : 3.8 Kg/cm2G Design Temp : 70℃ HLL 1m

2

5m

SUCTION LINE

1m

4”

ΔP 0.2 kg/cm

DISCHARGE LINE

Sp.Gr : 0.8 Viscosity : 0.3 Flowrate : 100 m3/Hr Suction Line ΔP 0.1 kg/cm2 Discharge Line ΔP 1.9 kg/cm2

0.8 0.3 100 m3/hr

2.22 kg/cm2.g ( P source-DP Suction) 8 kg/cm2.g 10.22 kg/cm2.g 12.12 3 kg/cm2.g 0.8 kg/cm2.g 2.2 m kg/cm2.g #VALUE! 83.7

FT 3”

5 kg/cm2.g 15 m

TEST 1. SUCTION PRESSURE OF PUMP ? 2. DP of Pump ? 3. Discharge Pressure Of Pump ? 4. ShutOff Pressure of Pump ? 5. Pressure Head (Destination P - Source P) 6. Elevation Head 7. Variable Loss (friction head) 8. DP of Control Valve 9. CV of Control Valve cv rated

38 ℃

1. Suction Press = (press tank 1+(head x sp.gr*0,1) - dp suction 2. dp of Pump = head x sp.gr x 0,1 head provided from pump curve ,for Q 100M3/HR head = 100 m

head= dp of pump=

100 m 8

3.discharge pressure P Dicharge 4. shutoff pressure of pump

10.22

maximal normal

shutoff press = max press ps + ph + normal flow shutoff press = normal press ps + ph + pd @ flo ps ph pd

5. presure head 6. elevation head

operation pressure of suction press high level of suctiion of suction vess differential pessure 3 kg/cm2.g

elevationhead =(high of vessel 2 - high of vesse elevationhead=

0.8 kg/cm2.g

7. variable loss (friction loss) friction loss = dpsuction + dp discharge +dp val

8. delta p of control valve dp of control valve = dp of pump -(press head + 9. cv of control valve cv rated cv

#VALUE! 83.7

5 TASK

15m

Suction Pressure of Pump?

I/P

ΔP of Pump? Discharge Pressure of Pump?

FT

Shutoff Pressure of Pump? Pressure Head(Destination P - Source P)?

3” ΔP 0.2 kg/cm2

Elevation Head?

FO

Variable Loss(Friction Head)?

.8 : 0.3 : 100 m3/Hr Line ΔP 0.1 kg/cm2 e Line ΔP 1.9 kg/cm2

ΔP of Control Valve? Cv of Control Valve?

*0,1) - dp suction

3/HR head = 100 m

C

kg/cm2.g

kg/cm2.g

press ps + ph + normal flow Pd mal press ps + ph + pd @ flow

12.12 kg/cm2.g

n pressure of suction press of suctiion of suction vessel minus centerline of pump

h of vessel 2 - high of vessel 1) x sp.gr x 0,1

tion + dp discharge +dp valve =

2.2 kg/cm2.g

= dp of pump -(press head + elevation head + friction head) kg/cm2.g

Source P)?

CONTROL VALVE FEBRUARY, 15-2019 DESIGN AND AVAILABLE DATA Design Pressure Design Temperature TANK 1 PRESSURE TEMPERATURE H.L Hs Hf Diameter

Delta P Suction Diameter

FT DP Delta P Discharge TANK 2 Pressure high FLUID PROPERTIES Sp.Gr Viscosity FLOW RATE

AGUNG PRABOWO 1507121393 UNIVERSITAS RIAU 3.8 kg/cm2.g (maximum) 70 C

2 kg/cm2.g 38 C 1m 5m 1m 4 Inch 10.16 cm 0.1016 m 0.1 kg/cm2.g 3 Inch 7.62 cm 0.0762 m 0.2 kg/cm2.g 1.9 kg/cm2.g

Design Pressure : 3.8 Kg/cm2G Design Temp : 70℃ HLL 1m

2

5m

SUCTION LINE

1m

4”

ΔP 0.2 kg/cm

DISCHARGE LINE

TEST 1. SUCTION PRESSURE OF PUMP ? 2. DP of Pump ? 3. Discharge Pressure Of Pump ? 4. ShutOff Pressure of Pump ? 5. Pressure Head (Destination P - Source P) 6. Elevation Head 7. Variable Loss (friction head) 8. DP of Control Valve 9. CV of Control Valve cv rated

0.027778 m3/s

27.77778 liter/s 13.88889

FT 3”

Sp.Gr : 0.8 Viscosity : 0.3 Flowrate : 100 m3/Hr Suction Line ΔP 0.1 kg/cm2 Discharge Line ΔP 1.9 kg/cm2

5 kg/cm2.g 15 m 0.8 0.3 100 m3/hr

38 ℃

2.777778

2.22 kg/cm2.g ( P source-DP Suction) 8.8 kg/cm2.g 11.02 kg/cm2.g 12.92 3 kg/cm2.g 0.8 kg/cm2.g 2.2 m 2.8 kg/cm2.g 62.37877 83.7

1. Suction Press = (press tank 1+(head x sp.gr*0,1) - dp suction 2. dp of Pump = head x sp.gr x 0,1 head provided from pump curve ,for Q 100M3/HR head = 100 m

head= dp of pump=

110 m 8.8

3.discharge pressure P Dicharge 4. shutoff pressure of pump

11.02

maximal normal

shutoff press = max press ps + ph + normal flow shutoff press = normal press ps + ph + pd @ flo ps ph pd

5. presure head 6. elevation head

operation pressure of suction press high level of suctiion of suction vess differential pessure 3 kg/cm2.g

elevationhead =(high of vessel 2 - high of vesse elevationhead=

0.8 kg/cm2.g

7. variable loss (friction loss) friction loss = dpsuction + dp discharge +dp val

8. delta p of control valve dp of control valve = dp of pump -(press head + 2.8 9. cv of control valve cv 62.37877 rated cv 83.7

5 TASK

15m

Suction Pressure of Pump?

I/P

ΔP of Pump? Discharge Pressure of Pump?

FT

Shutoff Pressure of Pump? Pressure Head(Destination P - Source P)?

3” ΔP 0.2 kg/cm2

Elevation Head?

FO

Variable Loss(Friction Head)?

.8 : 0.3 : 100 m3/Hr Line ΔP 0.1 kg/cm2 e Line ΔP 1.9 kg/cm2

ΔP of Control Valve? Cv of Control Valve?

*0,1) - dp suction

3/HR head = 100 m

C

kg/cm2.g

kg/cm2.g

press ps + ph + normal flow Pd mal press ps + ph + pd @ flow

12.92 kg/cm2.g

n pressure of suction press of suctiion of suction vessel minus centerline of pump

h of vessel 2 - high of vessel 1) x sp.gr x 0,1

tion + dp discharge +dp valve =

2.2 kg/cm2.g

= dp of pump -(press head + elevation head + friction head) kg/cm2.g

Source P)?

CONTROL VALVE FEBRUARY, 15-2019 DESIGN AND AVAILABLE DATA Design Pressure Design Temperature TANK 1 PRESSURE TEMPERATURE H.L Hs Hf Diameter

Delta P Suction Diameter

FT DP Delta P Discharge TANK 2 Pressure high FLUID PROPERTIES Sp.Gr Viscosity FLOW RATE

AGUNG PRABOWO 1507121393 UNIVERSITAS RIAU 3.8 kg/cm2.g (maximum) 70 C

2 kg/cm2.g 38 C 1m 5m 1m 4 Inch 10.16 cm 0.1016 m 0.1 kg/cm2.g 3 Inch 7.62 cm 0.0762 m 0.2 kg/cm2.g 1.9 kg/cm2.g

Design Pressure : 3.8 Kg/cm2G Design Temp : 70℃ HLL 1m

2

FT

5m

SUCTION LINE

3” 1m

4”

ΔP 0.2 kg/c

DISCHARGE LINE

Sp.Gr : 0.8 Viscosity : 0.3 Flowrate : 100 m3/Hr Suction Line ΔP 0.1 kg/cm2 Discharge Line ΔP 1.9 kg/cm2

5 kg/cm2.g 15 m 0.8 0.3 100 m3/hr

TEST 1. SUCTION PRESSURE OF PUMP ? 2. DP of Pump ? 3. Discharge Pressure Of Pump ? 4. ShutOff Pressure of Pump ? 5. Pressure Head (Destination P - Source P) 6. Elevation Head 7. Variable Loss (friction head) 8. DP of Control Valve 9. CV of Control Valve cv rated

38℃

2.22 kg/cm2.g ( P source-DP Suction) 3.2 kg/cm2.g 5.42 kg/cm2.g 7.32 3 kg/cm2.g 0.8 kg/cm2.g 2.2 m -2.8 kg/cm2.g #VALUE!

1. Suction Press = (press tank 1+(head x sp.gr*0,1) - dp suction 2. dp of Pump = head x sp.gr x 0,1 head provided from pump curve ,for Q 100M3/HR head = 100 m

head= dp of pump=

40 m 3.2

3.discharge pressure P Dicharge 4. shutoff pressure of pump

5.42

maximal normal

shutoff press = max press ps + ph + normal flow shutoff press = normal press ps + ph + pd @ flo ps ph pd

5. presure head 6. elevation head

operation pressure of suction press high level of suctiion of suction vess differential pessure 3 kg/cm2.g

elevationhead =(high of vessel 2 - high of vesse elevationhead=

0.8 kg/cm2.g

7. variable loss (friction loss) friction loss = dpsuction + dp discharge +dp val

8. delta p of control valve dp of control valve = dp of pump -(press head + -2.8 9. cv of control valve cv #VALUE! rated cv 83.7

5 TASK

15m

Suction Pressure of Pump?

I/P

ΔP of Pump? Discharge Pressure of Pump?

FT

Shutoff Pressure of Pump? Pressure Head(Destination P - Source P)?

3” ΔP 0.2 kg/cm2

Elevation Head?

FO

Variable Loss(Friction Head)? ΔP of Control Valve?

0.3 100 m3/Hr ne ΔP 0.1 kg/cm2 Line ΔP 1.9 kg/cm2

Cv of Control Valve?

,1) - dp suction

HR head = 100 m

C

kg/cm2.g

kg/cm2.g

ess ps + ph + normal flow Pd l press ps + ph + pd @ flow

7.32 kg/cm2.g

ressure of suction press f suctiion of suction vessel minus centerline of pump

of vessel 2 - high of vessel 1) x sp.gr x 0,1

on + dp discharge +dp valve =

2.2 kg/cm2.g

p of pump -(press head + elevation head + friction head) kg/cm2.g

Source P)?

FEB, 22 2019 By: AGUNG PRABOWO(1507121393) Teknik Kimia UNRI 2015 SIZING CONTROL VALVE FV3114 DIS PRESS = = SPILLBACK FLOW =

3.85 35 0.0097222222

kg/cm2 m3/h m3/s

Pipe 8" Pipe 6" Elbow 90

Length (m) 49.73 104.126 -

Diameter (m) 0.193675 0.1463294

Sum 1 1 23

Pipe 8" A v Re e e/D f dPf

= = = = = = =

0.0294839299 0.3297464837 4276.750088423 0.000046 0.0002375113 0.01 1735.522222483

m2 m/s m

385000

Pa

ID ID

7.625 5.761

45.7

in2

(Literatur) ( Geankoplis hal 88)

Pa

Elbow Kf hf dPf

= = =

0.75 0.029148378 2914.837797145

Pipe 6" A v Re e e/D f dPf

= = = = = = =

0.0168387434 0.5773721956 5657.80002138 0.000046 0.0003143592 0.0095 14008.37852882

Final Condition dPf total P Final

= =

19503.61906936 Pa 365496.3809306 Pa 3.6549638093 Kg/cm2

J/kg Pa

m2 m/s m

Tee n Kf hf dpf

= = = =

26.1

in2

(Literatur) (Dari Geankoplis hal 88)

Pa

Asumsi DP of Control Valve DP untuk CV maximum pada 30% dari total friksi pada aliran DP ASUMSI 5851.085720807 Pa 0.058511 Kg/cm2

Q SG k Cv

35 M3/hr 0.814 KG/L 1.167 152.3466372467

SG Densitas Viskositas RHO AIR

= = = =

INCH INCH

19.3675 14.63294

5 1 0.008449 844.8805

J/KG Pa

0.814 KG/L 796.906 kg/cm3 (Literatur) 0.0119 Pa.s (Literatur) 979

CM CM

0.193675 M 0.146329 M

4.2328

AGUNG PRABOWO 1507121393 Y-T0321 PRESSURE DSGN FLOW AREA VELOCITY FOR SUCTION SUCTION LENGTH PIPE DIAMETER FITTING ELBOW 90' DPF 45' DPF TEE DPF GATE VALVE 3/4 DPF GATE VALVE 10 DPF CHECK VALVE DPF TOTAL ELEVATION HEAD DPF DP SUCTION SUCTION PRESS

PUMP HEAD OF PUMP DISCHARGE LENGTH

Kg/cm2 35 M3/HR 0.009722 M3/S 74.6 INCH 0.048129 M2 0.202002873 M/S 10 inch 99.616 m 99616 9.75 inch 0.24765 m n 95.11988078 Pa n 44.3892777 Pa n 126.8265077 n 21.56050631 Pa n 21.56050631 Pa n 126.8265077 Pa 436.2831865 Pa

Sp.Gr T

2

Kf

0.75

hf 0.000951 J/KG

2

Kf

0.35

hf 0.000444 j/kg

2

Kf

1

hf 0.001268 J/KG

2

Kf

0.17

hf 0.000216 J/KG

2

Kf

0.17

hf 0.000216 J/KG

1

Kf

2

hf 0.001268 J/KG

0.004363 kg/cm2 -3.256 kg/cm2 kg/cm2 kg/cm2

4.5584 KG/CM2 #1

0.814 70

(press tank 321 +(head x

Kg/L C

(press tank 321 +(head x sp.gr x 0,1)- dp suction

(DARI KURVA POMPA UNTUK SPILLBACK

35 M3/HR