00-83T0040-220_Balance Of Plant – Material Balance

Contract No.

59/2009-EPC

Prepared

Checked

Approved

PROJECT : BIO-FUEL ETHANOL PLANT IN NORTHEN REGION LOCATION : TAM NONG, PHU THO, VIETNAM OWNER : PETROVIETNAM BIOFUELS JOINT STOCK COMPANY (PVB)

Document No.

00-83T0040-220

REV03

DATE: 11/06/10 SHEETS: 1 of 17

BALANCE OF PLANT - MATERIAL BALANCE

KMD

URL

ABGPROJECT SPECIFICATION

FOR APPROVAL

PD

DPD (Site)

Proc M

PM

PVC

Distribution

ALI

REV DATE PEM PREP’D CHK’D APP’D

0 22/12/09 S2 Gokul.K Nikhil.B A.Baxi

1 05/03/2010 S2 Gokul.K Nikhil.B R.Desai

2 13/4/2010 S2 Gokul.K Dattatray.G R.Desai

3 11/06/2010 S2 KMD URL ABGFOR APPROVAL

DESCRIPTION

FOR APPROVAL

FOR APPROVAL

FOR APPROVAL

PD

DPD (Site)

Proc M

PM

PM

EM

PEN

CVL

PIP

INST

ELC

DHT

S: Send Copy

PVC

Distribution

ALI

JVC

C: Circulation


OWNER PREPARED BY Gokul.K Gokul.K Gokul.K

LOCATION TAM NONG, PHU THO, VIETNAM CHECKED BY Nikhil.B Nikhil.B Dattatray.G

PROJECT BIO-FUEL ETHANOL PLANT IN NORTHEN REGION APPROVED BY A.Baxi R.Desai R.Desai

PROJECT No. 59/2009-EPC DATE 22/12/09 03/05/2010 13/4/2010

AREA No. PFD REVISION 0 1 2

2001 2002 2003 2004 2005 2006 2007 2008

RE

V

Raw Water from B/L

Raw Water to WTP

Potable Water for

Distribution

DM Water Make up to

Boilers

Process water to

Distribution

DM Water to DM Water

storage tanks

Effluent to Biomethana

tion Plant

Rejects from WTP

COMPONENT UNITS

2 Fresh Water kg/hr 502630.04 502630.04 1862.49 - - - - -

2 DM Water kg/hr - - 5600.00 - 12912.64 -

2 Effluent kg/hr - - - - 60723.01 60723.01

Process Water kg/hr - - - - 427131.90

PETROVIETNAM BIOFUELS JOINT STOCK COMPANY (PVB)

20 120

STREAM NUMBER

STREAM DESCRIPTION

2 Total Flow kg/hr 502630.04 502630.04 1862.49 5600.00 427131.90 12912.64 60723.01 60723.01

2 Design Flow kg/hr 502630.04 502630.04 1986.66 8741.13 427131.90 12912.64 60723.01 60723.01

(HOLD-3) (HOLD-3) (HOLD-4) (HOLD-3) (HOLD-3)

State - Liquid Liquid Liquid Liquid Liquid Liquid Liquid Liquid

Operating Pressure kg/cm2 g (HOLD-2) 4.5(HOLD-1) 4 3 4 1 2 2

Operating Temperature C 30 30 30 30 30 30 30 AMB.

Density kg/m3 995.68 993.34 993.33 993.31 993.33 993.28 993.30 993.30

HOLDS:

1) Vendor data awaited.

2) Alfa Laval / Client to confirm pressure at plant B/L.

3) Flowrates on hold, pending information of rejects from vendor.

4) DM Water make up flowrate given is excluding the losses in the steam circuit.

Page 2 of 17







3001

RE

V Cassava to Cleaning Section

Cassava Screen

Cassava Flour

COMPONENT UNITS

Cassava Chips kg/hr -

Screenings kg/hr -

Cassava Flour kg/hr 31500.00

STREAM DESCRIPTION

STREAM NUMBER


30 124

Total Flow kg/hr 31500.00

2 Design Flow kg/hr 37800.00

State - Solid

Operating Pressure kg/cm2 g ATM

Operating Temperature C AMB.

Density kg/m3 HOLD-1

HOLDs:

1) Vendor Data is awaited.

Page 3 of 17







4001 4002 4003 4004 4005 4006 4007 4008 4009 4010 4011

RE

V

Steam to PRS

Steam to Main

Process Plant

Steam to Main

Process Plant

Steam to Main

Process Plant

Steam to Dryer

Package

Steam to CO2

recovery Package

Flash Steam to

Boiler Package

from main process

plant

Boiler Blow Down to

Biomethanation plant

Boiler C.T. Blow Down

to Bio-Methanation

plant

Steam From

Power plant

Make up Process Water for

C.T. in Boiler Pkg.

COMPONENT UNITS

Steam kg/hr 31869.00 5340.00 15720.00 11060.00 9400.00 5400.00 3805.00 - - 46669.00 -

2 Water kg/hr - - - - - - - 200.00 17469.41 - 73506.42

(HOLD-1)


16240

STREAM NUMBER

STREAM DESCRIPTION

2 Total Flow kg/hr 31869.00 5340.00 15720.00 11060.00 9400.00 5400.00 3805.00 200.00 17469.41 46669.00 73506.42

2 Design Flow kg/hr 41925.00 5717.00 21426.00 15100.00 9400.00 5400.00 4682.00 200.00 17469.41 56725.00 73506.42

(HOLD-2) (NOTE-1) (HOLD-2) (HOLD-2)

State - Vapor Vapor Vapor Vapor Vapor Vapor Vapor Liquid Liquid Vapor Liquid

Operating Pressure kg/cm2 g 10 3.5 5 8 10 10 1 ATM. 2 10 4

Operating Temperature C 183.33 147.50 158.30 176.70 183.33 183.33 120.14 100 33 183.33 AMB.

Density kg/m3 5.55 2.39 3.13 4.6 5.55 5.55 1.13 957.97 992.58 5.55 993.33

(HOLD-2)

NOTES: HOLDS:

1) Flow is considering flow of steam for second investment stage also, steam is required for 18 to 21 hr /week. 1) Boiler blow down details on hold.

2) This is preliminary flow. Final Vendor data awaited.

Page 4 of 17







5001 5002 5003 5004 5005 5006 5007 5008 5009 5010 5011 5012

RE

V

CO2 from main process plant

CO2 to atm.

Process Water to Z-5001 & Z-

5002

Process Water to Z-5001

Process Water to Z-

5002 (Future)

Cooling Water supply to Z-

5001

Cooling Water

supply to Z-5002

(Future)

Cooling Water

Return from Z-5001

Cooling Water

Return from Z-5002

(Future)

Cooling Water Return to Z-

7001

Steam to Z-5001

Steam to Z-5002

(Future)

COMPONENT UNITS

CO2 kg/hr 11512.00 0.00 - - - - - - - - - -

Water kg/hr - - 74499.75 24833.25 49666.50 347417.00 694834.00 347417.00 694834.00 1042251.00 - -

Steam kg/hr - - - - - - - - - 1800.00 3600.00

STREAM DESCRIPTION

STREAM NUMBER


50 126

Total Flow kg/hr 11512.00 0.00 74499.75 24833.25 49666.50 347417.00 694834.00 347417.00 694834.00 1042251.00 1800.00 3600.00

Design Flow kg/hr 12000.00 12000.00 74499.75 24833.25 49666.50 347417.00 694834.00 347417.00 694834.00 1042251.00 1800.00 3600.00

(HOLD-1) (HOLD-1) (HOLD-1) (HOLD-1) (HOLD-1) (HOLD-1) (HOLD-1) (HOLD-1) (HOLD-1) (HOLD-1)

State - Vapor Vapor Liquid Liquid Liquid Liquid Liquid Liquid Liquid Liquid Vapor Vapor

Operating Pressure kg/cm2 g 0.05 ATM. 4 4 4 4 4 2 2 2 10 10

Operating Temperature C AMB. AMB. AMB. AMB. AMB. 33 33 41(HOLD-2) 41(HOLD-2) 41(HOLD-2) 183.33 183.33

Density kg/m3 1.92 1.83 993.33 993.33 993.33 992.62 992.62 990.47 990.47 990.47 5.55 5.55

(NOTE-1, 3) (NOTE-2) (NOTE-2)

NOTES: HOLDS:

1) Minimum flow shall be 0 kg/hr, after the installation of second package in future.

2) Flow of steam to the package is for 18 to 21 hr/day for 2 to 3 times a week.

3) During only first investment satge CO2 vented to atmosphere shall be around 7725 kg/hr.


2) Cooling water temperature is on hold.

Page 5 of 17







5013 5014 5015

RE

V

Effluent from Z-5001

Effluent from Z-5002

(Future)

Effluent to Biomethanation

Plant

COMPONENT UNITS

CO2 kg/hr - - -

Water kg/hr - - -

Steam kg/hr - - -

Effluent kg/hr 24833.25 49666.50 74499.75

STREAM DESCRIPTION

STREAM NUMBER


50 126

Total Flow kg/hr 24833.25 49666.50 74499.75

Design Flow kg/hr 24833.25 49666.50 74499.75

(HOLD-1) (HOLD-1) (HOLD-1)

State - Liquid Liquid Liquid

Operating Pressure kg/cm2 g 1 1 1

Operating Temperature C AMB. AMB. AMB.

Density kg/m3 993.28 993.28 993.28

HOLDS:


Page 6 of 17







6001 6002 6003 6004 6016 6017

RE

V

Sewage from septic

tanks

Sludge for Disposal

Treated Water to Disposal

Biogas to Boiler

Cooling Water return

to C.T. Z-7001

Process Water to Z-

6001

COMPONENT UNITS

Sludge kg/hr - (HOLD-2) - - - -

Treated Water kg/hr - - (HOLD-2) - - -

Biogas Nm3/hr - - - (HOLD-2) - -

2 Sewage water kg/hr 1500.00 - - - - -

Water kg/hr 395062.76 0.00


60 122

STREAM NUMBER

STREAM DESCRIPTION

2 Total Flow kg/hr 1500.00 (HOLD-2) (HOLD-2) 395062.76 0.00

2 Design Flow kg/hr 1500.00 (HOLD-2) (HOLD-2) 474472.36 29799.90

Total Flow Nm3/hr (HOLD-2)

Design Flow Nm3/hr HOLD-2

(HOLD-4) (HOLD-4)

State - Liquid Solid Liquid Vapor Liquid Liquid

Operating Pressure kg/cm2 g (HOLD-1) (HOLD-2) (HOLD-2) 2.5(HOLD-2) 2 4

Operating Temperature C 30 (HOLD-2) (HOLD-2) (HOLD-2) 41 AMB.

Density kg/m3 995.68 (HOLD-2) (HOLD-2) (HOLD-2) 990.47 993.33

(HOLD-3)

HOLDS:

2 1) Data will be confirmed during detail engineering.

2) Vendor inputs awaited. 4) This is preliminary flow. Final Vendor data awaited.

3) Flow is assuming 100 persons per shift and consuming 150 liters/person/day water. 80% of supplied water is considered as effluent.To be confirmed during Detail Engineering.

Page 7 of 17







6005 6011 6012

RE

V

Whole Stilage to Decanter

Thin Slop recycle to

Main Process

Plant

Thin Slop to Bio-

Methanation Plant

COMPONENT UNITS Case A Case B Case A Case B Case A Case B Case A Case B Case A Case B

2 Suspended Solids kg/hr 2677.77 669.44 669.44 2008.33 2008.33 2008.33 2008.33 2008.33 2008.33 - - 270.50 669.44

2 Liquid with dissolved solids kg/hr 83948.23 77969.55 79370.09 5978.68 4578.15 5978.68 4578.15 654.01 553.08 5324.67 4025.07 33697.00 83395.16

Condensate from Dyer to Thin Slop Tank

6009 6010


60 157

Dry Cake to Storage

6006 6007 6008

Thin Slop from Decanter Wet Cake from Decanter Wet cake to StorageSTREAM DESCRIPTION

STREAM NUMBER

2 Total Flow kg/hr 86626.00 78638.99 80039.53 7987.01 6586.48 7987.01 6586.48 2662.34 2561.41 5324.67 4025.07 33967.50 84064.60

2 Design Flow kg/hr 102823.00 93342.61 95005.02 9480.39 7817.98 9480.39 7817.98 3160.13 3040.33 6320.26 4777.65 33967.50 99782.67

State - Liquid Liquid Liquid Solid Solid Solid Solid Solid Solid Liquid Liquid Liquid Liquid

Operating Pressure kg/cm2 g 1 0.5 0.5 ATM. ATM. ATM. ATM. ATM. ATM. 0.5 0.5 4 2

Operating Temperature C 80.6 80.6 80.6 80.6 80.6 80.6 80.6 Note 1 Note 1 Note 1 Note 1 80.6 80.6

Density

kg/m3

970.50 970.50 970.50

600-750 HOLD-1

600-750 HOLD-1

600-750 HOLD-1

600-750 HOLD-1 Note 1 Note 1 Note 1 Note 1 970.50 970.50

(NOTE-2) (NOTE-2) (NOTE-3)

NOTES: HOLDS:

1) Vendor to confirm. 2) This is intermediate stream applicable only in the case of dryer failure. 1) Density of Wet Cake to be confirmed by Vendor.

Case A: 30 % w/w Total Solids content; Case B: 35 % w/w Total Solids Content3) Thin slop will either be transferred to the Main process plant or to Cassava preparation & desanding area.

Page 8 of 17







6013 6014 6015 6016

RE

V

Condensate from Dryer

Thin Slop recycle to

Slurry preparation &

Desanding area

Cooling Water

Return from Dryer

Whole Stillage

recirculation to Whole

Stillage Tank

COMPONENT UNITS

Steam kg/hr - - - -

Condensate kg/hr 9400.00 - - -

Cooling Water kg/hr - - 482413.32 -

2 Suspended Solids kg/hr - 270.50 - 599.77

2 Liquid with dissolved solids kg/hr - 33697.00 - 18810.23

STREAM DESCRIPTION

STREAM NUMBER


60 157

2 Total Flow kg/hr 9400.00 33967.50 482413.32 19410.00

2 Design Flow kg/hr 9400.00 33967.50 482413.32 19410.00

(HOLD-2)

2 State - Liquid Liquid Liquid Liquid

2 Operating Pressure kg/cm2 g 8 4 2 1

2 Operating Temperature C 175 80.6 41 80.6

2 Density kg/m3 892.23 970.50 990.47 970.5

(HOLD-1) (NOTE-1)

HOLDS: NOTES:

1. Operating conditions are on hold. Data is awaited from dryer vendor.

2. This is preliminary flow. Final Vendor data awaited.

1) Thin slop will either be transferred to the Main process plant or to Cassava preparation & desanding area.

Page 9 of 17







STREAM NUMBER 7001 7002 7003 7004 7029 7030 7031 7032 7033 7034 7035 7036 7048

RE

V

STREAM DESCRIPTION

Process Water Make up to C.T. Z-

7001

Cooling Water from

PC-7001A/B/C/

D

Cooling Water

Return to C.T. Z-7001

Cooling Tower Blow down to Bio-methanation

Plant

Process Water Make up to C.T. Z-

7008

Cooling Water from

PC-7020A/B/C

Cooling Water

Return to C.T. Z-7008

Cooling Tower

Blowdown to

Biomethanation Plant

Cooling Water

Supply to CO2

recovery Pkg.

Cooling Water

Supply to Dryer Z-

6002

Cooling Water

Supply to IA/PA

System

Cooling Water

Supply to Chiller Unit

Z-7004

Cooling Water

Supply to Chiller Unit

Z-7007

COMPONENT UNITS

Fresh Water kg/hr 42726.09 - - - - - - - -

2 Cooling Water kg/hr - 5741094.46 5741094.46 24595.88 84433.05 4428175.98 4428175.98 37223.97 1042251.00 482413.32 29778.60 282896.70 3484096.20


70 137,167

2 Total Flow kg/hr 42726.09 5741094.46 5741094.46 24595.88 84433.05 4428175.98 4428175.98 37223.97 1042251.00 482413.32 29778.60 282896.70 3484096.20

2 Design Flow kg/hr 110292.93 5820504.06 5820504.06 24595.88 84433.05 4870993.58 4870993.58 37223.97 1042251.00 482413.32 29778.60 282896.70 3484096.20

(HOLD-3) (HOLD-3) (HOLD-3) (HOLD-3) (HOLD-3) (HOLD-3) (HOLD-3) (HOLD-3) (HOLD-3)

State - Liquid Liquid Liquid Liquid Liquid Liquid Liquid Liquid Liquid Liquid Liquid Liquid Liquid

Operating Pressure kg/cm2 g 2 4 2 2 2 4 2 2 4 4 4 4 4

Operating Temperature C AMB. 33 41 33 AMB. 33 34.9 34.9 33 33 33 33 33

Density kg/m3 993.63 992.62 990.47 992.57 993.33 992.62 992.11 992.11 992.62 992.62 992.62 992.62 992.62

HOLDS:

1) DELETED.

2) DELETED.


Page 10 of 17







7049 7051 7052

RE

V

Cooling Water

Return from Z-7007

Cooling Water

Supply to Biomethana

tion Plant

Cooling Water to

Main Process Plant @

30°C

COMPONENT UNITS

Fresh Water kg/hr - - -

2 Cooling Water kg/hr 3484096.20 395062.76 4428175.98


70 137,167

STREAM NUMBER

STREAM DESCRIPTION

2 Total Flow kg/hr 3484096.20 395062.76 4428175.98

2 Design Flow kg/hr 3484096.20 474472.36 4870993.58

(HOLD-1) (HOLD-1)


Operating Pressure kg/cm2 g 2 4 3

Operating Temperature C 41 33 30

Density kg/m3 990.47 992.62 993.31

HOLDS:


Page 11 of 17


OWNER PREPARED BY Gokul.K Gokul.K Gokul.K K M D

LOCATION TAM NONG, PHU THO, VIETNAM CHECKED BY Nikhil.B Nikhil.B Dattatray.G U R L

PROJECT BIO-FUEL ETHANOL PLANT IN NORTHEN REGION APPROVED BY A.Baxi R.Desai R.Desai A B G

PROJECT No. 59/2009-EPC DATE 22/12/09 03/05/2010 13/4/2010 11/06/2010

AREA No. PFD REVISION 0 1 2 3

STREAM NUMBER 7005 7007 7008 7009 7010 7011 7012 7041 7042 7039 7040 7043 7044

RE

V

STREAM DESCRIPTION

Bio-EtOH from

Process Plant

Bio-EtOH to Static Mixer

Off-Spec Bio-EtOH to

Process Plant

Denat. from tanker

Denat. To Mixer

Denatured Bio-EtOH to

Storage

Comm. Bio-EtOH to Truck

Loading

Bio-EtOH vapors from

TK-7001A/B/C

Bio-EtOH Condensate

from E-7001A/B/C

Chilled Water

Return from E-7001A/B/C

Chilled Water

Return from E-7004A/B

Bio-EtOH Vapours from TK-7004A/B

Bio-EtOH Condensate

from E-7004A/B

COMPONENT UNITS

3 Ethanol kg/hr 10874.00 65422.50 3708.00 - - 65422.50 118852.50 36.00 26.00 - - 395.00 269.00

Denaturant kg/hr - - - 15600.00 3217.50 3217.50 - - - - - - -

3 Water kg/hr - - - - - - - - - 7200.00 50550.00 - -

3 Air kg/hr - - - - - - - 96.00 - - - 1215.00 -


70 131,168,169

3 Total Flow kg/hr 10874.00 65422.50 3708.00 15600.00 3217.50 68640.00 118852.50 132.00 26.00 7200.00 50550.00 1610.00 269.00

3 Design Flow kg/hr 11895.00 71964.75 4450.00 17160.00 3539.25 75504.00 130737.75 132.00 26.00 7200.00 50550.00 1610.00 269.00

3 (NOTE-3,4) (NOTE-3,4) (NOTE-1) (NOTE-2) (NOTE-3,4) (NOTE-3,4)

3 State - Liquid Liquid Liquid Liquid Liquid Liquid Liquid Vapour Liquid Liquid Liquid Vapour Liquid

3 Operating Pressure kg/cm2 g 2.5 3 7 3 3 2 3 ATM. ATM. 2.90 2.90 ATM. ATM.

3 Operating Temperature C AMB. AMB. AMB. AMB. AMB. AMB. AMB. 40.00 21.00 18.00 18.00 40.00 21.00

Densitykg/m3

793.00 793.00 793.00780

(HOLD-2)780

(HOLD-2) 792.35 792.35 1.25 793.00 995.89 995.86 1.25 793.00

(4hr/day) (4hr/day) (4hr/day)

HOLDS: NOTES:

3 1) DELETED.

3 2) Flowrate given is considering flow to both exchangers continuously. 4) Flowrate considered is for worst case scenario & is intermittent.

1) Flowrate given is considering flow to all 3 exchangers continuously. 3) Flowrate given is for 1 tank & its exchanger.

2) Data to confirmed during detail engineering.

Page 12 of 17







STREAM NUMBER 7053 7054 7055 7056

RE

V

STREAM DESCRIPTIONVapours

out from E-7001A/B/C

Vapours out from E-

7004A/B

Fusel Oil from Main Process

Plant

Fusel Oil to Tanker

COMPONENT UNITS

3 Ethanol kg/hr 10.00 126.00 - -

3 Air kg/hr 96.00 1215.00 - -

2 Fusel Oil kg/hr 55.77 16167.00


70 131,169,362

3 Total Flow kg/hr 106.00 1341.00 55.77 16167.00

3 Design Flow kg/hr 106.00 1341.00 64.66 17783.70

3 (NOTE-1,2) (NOTE-1,2) -

3 State - Vapour Vapour Liquid Liquid

3 Operating Pressure kg/cm2 g ATM. ATM. 0.5 2

3 Operating Temperature C 21.00 21.00 AMB. AMB.

3 Density kg/m3 1.25 1.25 808.25 808.35

NOTES:

3

3 2) Flowrate considered is for worst case scenario & is intermittent.

1) Flowrate given is for one exchanger.

Page 13 of 17







7013 7014 7015 7016 7028 7037 7038 7050 7047

RE

V

Process Water to Chilled Water

TK-7011

Chilled Water @ 21°C to

Main Process

Plant

Chilled Water @ 15°C to Users

Chilled Water return

@ 28.5°C from Main Process

Plant

Process Water to

Chilled Water TK-7010

Chilled Water @

15°C to E-7001A/B/C

Chilled Water @

15°C to E-7004A/B

Chilled Water @ 15°C to

Main Process

Plant

Cooling Water

Return from Chiller Unit

Z-7004

COMPONENT UNITS

Fresh Water kg/hr 11341.00 - - - - - - -

3 Chilled water kg/hr - 80633.88 11341.00 80633.88 7200.00 50550.00 11341.00 282896.70


70 140

STREAM NUMBER

STREAM DESCRIPTION

3 Total Flow kg/hr 11341.00 80633.88 11341.00 80633.88 7200.00 50550.00 11341.00 282896.70

3 Design Flow kg/hr 17937.36 80633.88 17937.36 80633.88 7200.00 50550.00 17937.36 282896.70

(HOLD-1)

3 State - Liquid Liquid Liquid Liquid Liquid Liquid Liquid Liquid

3 Operating Pressure kg/cm2 g 1.5 3 3 1.5 3 3 3 2

3 Operating Temperature C AMB. 20 15 30 15 15 15 41

3 Density kg/m3 993.29 995.48 996.52 993.29 996.52 996.52 996.52 990.47

HOLDS:


Page 14 of 17







STREAM NUMBER 7017 7018 7019 7020

RE

V

STREAM DESCRIPTIONSteam Cond.

To Boiler

Steam Conden. Return to

Boiler package

Steam Cond. from

Main Process

plant

Steam Cond. to

Desuperheater

COMPONENT UNITS

Steam kg/hr - - -

Water kg/hr 37463.50 37715.00 251.50


14770

Total Flow kg/hr 37463.50 37715.00 251.50

Design Flow kg/hr 46643.50 46961.00 317.50


Operating Pressure kg/cm2 g 2 1 7 (HOLD-1)

Operating Temperature C 120.14 120.14 120.14

Density kg/m3 942.95 942.9 943.55

HOLDS:

1) Pressure of steam condensate to Desuperheater is on hold.

Page 15 of 17







7021 7022 7025 7026 7027

RE

V

H2SO4 in from

Tanker

H2SO4 to Main

Process plant

Aq. Ammonia

from Tanker

Aq. Ammonia to

Process Plant

Nitrogen from

Nitrogen cylinder bank

COMPONENT UNITS

H2SO4 (98%) kg/hr 27600.00 9200.00 - -

N2 kg/hr - - - -

Aq. NH3 (30%) kg/hr - - 13500.00 900.00


70 134,170,171

STREAM NUMBER

STREAM DESCRIPTION

Total Flow kg/hr 27600.00 9200.00 13500.00 900.00

Design Flow kg/hr 30360.00 10120.00 14850.00 990.00

State - Liquid Liquid Liquid Liquid

Operating Pressure kg/cm2 g 2 2 2 2

Operating Temperature C AMB. AMB. AMB. AMB.

Density kg/m3 1840 1840 900 900

(NOTE-1,2) (NOTE-1)

HOLDS: NOTES:

1) DELETED.

2) H2SO4 will either be transferred to the Main process plant or the WTP.

1) Requirement is intermittent.

Page 16 of 17







7045 7046

RE

V Cooling Water

Return to Z-7001

IA to distribution

COMPONENT UNITS

Instrument Air Nm3/hr - 1939

Water kg/hr 29778.60 -


70 143

STREAM NUMBER

STREAM DESCRIPTION

Total Flow kg/hr 29778.60 1939

Design Flow kg/hr 29778.60 2326

(HOLD-1) (HOLD-1)

State - Liquid Gas

Operating Pressure kg/cm2 g 2 9

Operating Temperature C 41 AMB.

Density kg/m3 990.47 11.32

HOLDS:


Page 17 of 17

Documents

00-83T0040-220_Balance Of Plant – Material Balance