Hot Crude Oil Storage.xls

7/22/2019 Hot Crude Oil Storage.xls

1/13

Art Montemayor Crude Oil Project August 12, 2002

Rev: 0

Summary of relief calculations for T-400 & T-405

1. The Rainstorm with subsequent vacuum is the controlling case for relief.Since both tanks operate without Conservation Valves and with Open Vents, the vacuum demandfor the controlling case is more than sufficient for the worst pressure case (the Fire Case);

2. The amount of open vent capacity required for the worst case (rainstorm) is to be handled byinstalling four (4) - 12" Open Vents on the roof of each tank; these vents should have a Flamearrestor under a 180o return. The vent outlet should have a Stainless Steel screen to keep outforeign objects and to resist corrosion.

3. The flame arrestors should have a nominal capacity for 2.55 MM scfh each such that they do notcreate a pressure drop in excess of what the tank design vacuum can withstand at the existingatmospheric pressure.

4. The four open vents should be located at equal 90o quadrant locations on the roof in order to allowequal distribution of created pressure or vacuum conditions.

Page 1 of 13FileName: 161245513.xls.ms_office

WorkSheet: Summary of Results


2/13

Art Montemayor Oil Recovery November 24, 2001

Rev: 2(06/11/02)

Stored Material

Flash PointoF 350 (Estim.) in WC 55.36

Boiling PointoF 360 (Estim.) oz/in

20.50

Latent Heat vap. Btu/lb 144.0 (Hexane) ft 50.0Mol. Wt. 274.0 ft 30.0

Inflows

Flow, GPM

Value Units Note 1

P-160/-170 -106C 100 PSIG 1,200

P-165/-175 -107C 50 PSIG 1,200

2,400

or :

or : 100 psi

or :

2,400

1,500

Outflows (See Note 1)

Capacitygpm 2,500

gpm 2,500

gpm

Total 5,000

Notes:

Tag

10"-PL-138-A

MAWP

Max Vacuum

DiameterMax fill

Tag

T - 400 & T - 405

Transfer to Storage

Transfer to Storage 10"-PL-055-A

Total Inflows, gpm

Tank Padding Calculation Sheet

Attachment 1

P &ID #

115-XXX-

01

Max HeadService Line No.

Data Entry

Crude Oil Tank

2) The above pump capacities are estimated due to a lack of pump performance curves.

Sonic Flow in Pipe

Pipe Flow at Maximum DP

Other (Attach Method)

Use for Relief (gpm)

Normal Maximum (gpm)

P-410

P-420

1) Pumps are at zero head flowrate (Max. gpm), and Control Valves have the max. trim size (Max. C v)

Page 2 of 13Electronic FileName: 161245513.xls.ms_office

WorkSheet: Data Entry


3/13


Rev: 4(04/20/08)

Flash PointoF 350 (Estim.) in. WC 55.4

Boiling PointoF 360 (Estim.) oz/in

20.5

Latent Heat Vap. Btu/lb 144 (Hexane) ft 50.0

Molecular Wt. 274 ft 30.0

gal 440,620ft

23,927.0

12,861

20,578 Fire BTU/hr-ft2

4,735

SCFH 690,425

40,104

SCFH 0

SCFH 58,642

Out SCFH 6,295

In SCFH 10,491 MM Scfh 10.2

N.A. in WC

Required SCFH NAselected SCFH NA

Fail Open SCFH 0

Required SCFH N. A.

Selected SCFH N. A. Regulator w/ " trim.

Valve Fail Open SCFH N. A.

Inflow (Pressure) SCFH 85,515

Fire (Pressure) SCFH 690,425

Outflow (Vacuum) SCFH 10,232,913

1)

2)

3)

4)

MAWP

Diameter

This flowrate assumes the valve's Cv determines the capacity

Consider this only if the tank vents to a vacuum source or header

Normal Operation

Outflows, SCFH

Blow-Through From Upstream

Refer to API-2000; 5th

Ed., April 1998; Table 2A for thermal breathing requirements.

Tank Pressure & Vacuum ProtectionDesign Sheet - Based on Data Entry Sheet

Notes:

Required Capacity

Stored Material:

Wetted Area

Max fill Height

Max fill Volumenflows, SCFH (see API 2000; table 1A)

Attachment 2

Pool Fire Case

T - 400 & T - 405Crude Oil

Max Vacuum

Tank:

Rain Storm CoolingVacuum (Note 3)

Relief Scenario Unit Heat Input

Flashing Feed (Note 4)Thermal Breathing, Note 1

Pump Inflow + Out Breathing + Flashing Feed

Consider this when using emission vapor control system

Pumps' outflows + in Breathing + condensed vapor during rainstorm

Blanket Gas Valve set at 7" WC

With vent system Pressure Drop of 9 in WC

Vent Valve set at

sum of outflows + in Breathing + fail open vent valve

Pressure and Vacuum Relief Cases

Fisher Model

Normal max inflow + out breathing

These two Crude Oil Storage Tanks (T-400 & T-405) should be equipped with 4- 12" roof nozzles located

at a convenient location. The nozzle should have a Flame arrestor sized for 2,500,000 Scfh and a 180o

return with a protective stainless steel screen.

Fire Case calculations are according to API Standard 2000, 5th

Ed., Section 4.3.3.2.1

Internal vapor condensation during a Tropical rainstorm is a special case detailed in this worksheet.

The Hot Crude Oil introduced into these tanks goes through a Vapor Separator where some flash vapor is

removed and routed to vapor disposal; however some additional vapor remains in equilibrium with the

crude and flashes inside the main tank that is vented directly to the atmosphere.

Page 3 of 13

Electronic FileName: 161245513.xls.ms_office

WorkSheet: Design Basis


4/13


Rev: 2(06/11/02)

TANK:

in. W.C. Rated at in. W.C.

Required SCFH

Selected Size SCFH (Note 2) Total 0

oz/inRequired SCFH 10,232,913

Selected Capacity SCFH (Note 2) Total 0

Set at in. W.C. Rated at in. WC

Required SCFH 0

Selected Size SCFH N. A. Total

Set at oz/in Rated at in. WC

Required SCFH 424,263

Selected Size SCFH N. A. Total

Tag Size, in Cv

N. A. 2 66.7

N. A.

N. A.

N. A.

N. A.

1)

2)

3)

section 4.2.5.14, "Uninsulated Tanks"

Attachment 3

Fisher 1190

zero (if Con vent has capacity) or Worst case w/o Con Vent

each from catalog; total number

Manufacturer Model

T - 400 & T - 405

Conservation Vent

Blanket Gas Regulator

Nitrogen Valve

Conservation Vent

Emergency Pressure Relief, Note 1

These tanks are designed taking into consideration the recommendations of API Standards 2000, 5th Ed.;

Selected Equipment:

Emergency Vacuum Relief

zero (if Con vent has capacity) or Worst case w/o Con Vent


Emergency Vent

Storage Tank Pressure/Vacuum Equipment Specifications

Vacuum Side set at 0.5 oz/in2 Vacuum, rated at

Pressure side set at

zero (if tank has Vent Valve and Emergency vent) or worst case


Outflow Case


A Conservation vent (PVSV) is not recommended for these two crude oil storage tanks.

For technical calculations and process analysis determining the type and degree of tank pressure and vacuum

protection, refer to included worksheets "Condensing Vapor".

A Fire hatch or Emergency Vent is not required since the open 12" vents on this tank have sufficient capacityfor the controlling case (vacuum) and this is sufficiently large for the worst pressure case also.

Notes:

Emergency Vacuum

Page 4 of 13


WorkSheet: Requisition Info


5/13


Rev: 4(04/20/08)

Storage Tank:

Fluid:

1 Liquid movement in 20,578 20,578 N.A. N.A.

2 Liquid movement out N.A. N.A. N.A. 40,104 N.A.

3 Out Breathing (Vapor out) 6,295 N.A. N.A. N.A.

4 In Breathing (Vapor In) 10,491 N.A. 10,491 N.A.

5 Fire Exposure 690,425 N.A. N.A. N.A.

6 Pressure Transfer Blow-through N.A. N.A. N.A. N.A. N.A.

7 Blanket Gas Failure - Blocked N.A. N.A. N.A. N.A.

8 Blanket Gas Failure - Open N. A. N. A. N.A. N.A. N.A.

9 Steam Coil Rupture N.A. N.A. N.A. N.A. N.A.

10 Vent System Failure - Blocked N.A. N.A. N.A. N.A. N.A.

11 Chemical Reaction N.A. N.A. N.A. N.A. N.A.12 Flashing Feed (Note 2) N.A.

13 Steam-Out N.A. N.A. N.A. N.A. 13,566,429

26,873 700,916 50,595 13,566,429 0

876,145

63,244

Air density = 0.0807 lb/ft3 at 32 oF and 14.696 psiaBlanket gas density = 0.33425 lb/ft

3at 109

oF and 79.7 psia

Blanket gas Molecular Weight = 25.237

Blanket gas density = 0.083877 lb/ft3

at 109oF and 20 psia

Blanket gas specific gravity = 1.0394 lb/ft3

at 109oF and 20 psia

case because an open, atmospheric vent is employed which is designed for the controlling vacuum case.

Note 2: Although the crude oil feed is flashing into the tank, this case is not a credible pressure

steaming out the tank. The open vents capacity plus the roof manway should suffice for the steam out.

cfh (Includes 25% contingency)

cfh (Includes 25% contingency)

Note 1: The steam-out case is calculated in this Workbook; relief protection is recommended

Controlling Vacuum Case Design Capacity =

T - 400 & T - 405

Attachment 4

Case Contributions:

in the form of a properly sized nozzle (or roof-located manway) that is required to be left open while

Other

Vacuum ScenarioPressure Scenario

Steam-Out

(Note 1)

OutflowInflow Fire Case

Controlling Pressure Case Design Capacity =

Crude Oil

Total Volumetric Flow:

Safety Scenario Relief Rates, CFH

Liquid

Overflow

Page 5 of 13


WorkSheet: Case Summaries


6/13

Art Montemayor Storage Tank Pressure Relief

Over-Pressurization Scenario Contributions

November 22, 2001

Rev: 2(06/11/2002)

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

No. Event Press. Vacuum Press. Press. Press. Press. Press. Press. Press. Press. Press. Press.

1 Liquid Movement in and Breathing Out Yes No No No No Note 2 Note 2 No Note 2 No No No

2 Liquid Movement Out and Breathing In No Yes No No No Note 2 Note 2 No Note 2 No No No

3 Fire Exposure No No Yes No No No No No No No No No

4 Pressure Transfer Blow Through No No No No No No No No No No No No

5 Blanket Gas Regulator Failure No No No No No No No No No No No No6 Failure or Loss of Control - Heat Transfer Devices No No No No No No No No No No No No

7 Failure of Internal Heating / Cooling Coils No No No No No No No No No No No No

8 Failure of Vent Treatment System No No Note 1 No No No No No No No No No

9 Failure of Utilities (Steam, Nitrogen, air, CWS) No No No No No No No No No No No No

10 Chemical Reaction No No Note 3 No No Note 3 Note 3 No Note 3 Note 3 No Note 3

11 Liquid Overfill No No No No No No No No No No Yes No

12 Flashing Liquid Feed Yes No No No No No No No No No No Yes

13 Steam Out (Note 4) N. A. N. A. N. A. N. A. N. A. N. A. N. A. N. A. N. A. N. A. N. A. N. A.

1)

2)

3)

4)

omments on scenarios for Tank T - 400 & T - 405:

Steam Out is a special case that is handled and calculated independently in this Workbook; a properly sized nozzle is usually specified to be left open for this case.

Consider Event when calculating CASE:

Consider this event if the fluids involved normally, or potentially, can cause a reaction

This event is when the vent valve feeding tank vapors to a vapor treatment system fails closed.

Either or both liquid movement events could be applicable dep

otes:

Event No. 11 is not considered a credible scenario since the tank has been designed according to API Standard 2000, 5th Ed.; article 4.2.5.10

Event No. 10 is not considered a credible scenario since the compounds and fluids with potential for introduction into the tank do not react with each other or polimerize.

Event No. 4 is not considered a credible scenario since all liquid transfer into tank is done by pumping, not pressure transfer.

Event No. 6 is not considered a credible scenario since this tank does not incorporate a heat transfer device or internal coil.

Event No. 7 is not considered a credible scenario since this tank does not incorporate an internal coil that could rupture.

Event No. 8 is not considered a credible scenario since this tank does not incorporate a Vapor Treating System.

Page 6 of 13Electronic FileName: 161245513.xls.ms_office

WorkSheet: OverPressure Scenarios


7/13

Art Montemayor Storage Tank Pressure Relief May 14, 2002

Rev: 2(06/11/2002)

Event Inflow / Outflow

Liquid Movement in and Breathing Out Inflow

Liquid Movement Out and Breathing In Outf low

Exposure to Pool Fire with subsequent

tank contents' vaporization

Inflow

Pressure Transfer Blow-through Inflow

Inert Gas Pad/Purge Regulator Failure Inf low

Failure or loss of Control Heat Transfer

Devices

Either or both

Failure of Internal Heating/Cooling Coils Either or both

Failure of Vent Treatment System Outflow

Failure of Utilities (Air, Steam, Cooling

Water, N2, etc.)

Either or both

Chemical Reaction Inflow

Liquid Overfill Inflow

Flashing Liquid Inflow

Determination

for use when calculati


WorkSheet: Inflow-Outflow


8/13

Art Montemayor Storage Tank Pressure Relief May 14, 2002

Rev: 2(06/11/2002)

Calculate Inflow or Outflow by:

termine the Maximum flow, at zero head, for each pump that can be lined up to the tank. For sources

t are not pump driven, calculate the maximum flow for the flow limiting element. For Control valves,

e the largest trim for the valve body and add the capacity of any bypass valves. The total inflow is the

m from all of these sources. The total inflow can be reduced if engineering judgment indicates that it is

kely that all of the sources will be feeding into the tank simultaneously. The total inflow can also be

uced if the pressure drop in the line(s) between the inlet manifold(s) and tank exceeds the available

ssure drop. The available pressure drop is the highest pressure sources dead head pressure.

termine the Maximum flow, at zero head, for each pump that can take suction from the tank. The

tflow is the sum of all of these; even installed spare(s).

not consider inflow for fire case since there is ample time to shutoff the inflow before the fire case fully

velops. (see also API-2000 3.4.3.1.4) Do consider the failure of the blanketing gas regulator (if

plicable) since these instuments typically fail open and the heat from a fi re could cause it to fail.

e Case 1

e Case 1

e Case 1 if the failure can cause the tank to vent. Use Case 2 if the failure can create a vacuum in the

k.


k.

e case 2


k.

e Case 1

Project Tanks will be designed according to API Standard 2000, 5th Ed.; article 4.2.5.10

en introducing flashing liquids, always include the flashed vapor in the total relief capacity.

Inflows and Outflows for Storage Tanks

Normal and Emergency Venting Requirements


WorkSheet: Inflow-Outflow


9/13

Art Montemayor Project

Crude Oil Storage Vacuum Relief

June 03, 2001

Rev: 0

50.00 feet

32.00 feet

62,832 Ft3

47,124 Ft3

= 9,817 Ft3

56,941 Ft3

Assume that the blanket vapor regulator fails in the closed position and that the flashing feed continues to enter

the Crude Oil storage tank, effectively sweeping out the non-condensibles through the PVSV pressure side.

Under these conditions, it is feasible for the vapor space to essentially become water vapor ("steam") rich

in composition after a prolonged period of saturated Crude Oil entering the tank proper and flashing.

It is at this critical moment that a credible tropical rainstorm could develop and drench the area for hours.

From the process simulation run of Nov 27, 2001 the Crude Oil Flash vapor produced in the storage tank due to

adiabatic expansion is:

208oF

14.7 psia

0.040864 Lb/ft3

1.407 MM Scfd = 1.773 MM Acfd

19.788

3,058 Lb/hr

Mole %

92.96

7.04

The storage tank surface area capable of cooling-condensing the vapors when the tank is 25% full is:

3,770 ft2

1,991 ft2

5,760 ft2

In accordance with API Standard 2000, paragraph 4.2.5.14 - "Uninsulated Tanks":

Tank's Water Vapor volume @ 25% full =

Cylindrical tank section with fuel gas blanket =

Conical roof volume with fuel gas blanket = (3.1416 r2) (h) / 3

out by their respective booster pumps and a sudden rainstorm develops.

of the water vapor in the vapor space which will can be at a temperature between 180oF to 220

oF.

The concern for this scenario occuring is due to the partial vacuum hazard created by the condensation

is equal to the rate of condensed water vapor during the rainstorm due to heat transfer through the tank's roof

Tank Height =

Since the Crude Oil Storage is being fed with a flashing crude oil feed that is adding water vapor ,

there is a possibility that a partial vacuum can be created as the continuing tanks' operation is being pumped

The storage tanks could normally be filled with a minimum of approximately 25% of the total available

tank height.

Total (100%) Tank cylindrical Volume =

This situation would be in the worse circumstance if the tank were almost empty at the moment the rain

commences. The rate of atmospheric air required to maintain the tank at the minimum design pressure

Pressure

Cone top roof surface area =

Total Surface Area =

Vapor Flowrate

Total Molecular Weight

Total Flowrate

Crude Oil Tank Diameter =

Tanks T-400 & T-405

Non-condensables

Cylindrical surface area =

and wall in contact with the internal vapor.

Vapor Density

Temperature

Total Stream Composition:

Water

Page 9 of 13

FileName: 161245513.xls.ms_office

WorkSheet: Condensing Vapor


10/13

Art Montemayor Project

Crude Oil Storage Vacuum Relief

June 03, 2001

Rev: 0

Where,

Q =

U =

A =

DT =

500

Q = 368,666,833 Btu/hr

379,951 lb/hr

= 190 ton/hr

26.799 ft3/lb

ft3/hr

= 244.4 MM Acfd

= 169,705 ft3/min

= 2,828 ft3/sec

Although the above scenario is agravated by the Crude Oil pumped out by the booster pumps at a maximum

rate of 40,100 cfh (approximately 1.0 MM cfd) this effect will be short-lived due to the fact that as the tank

develops a vacuum condition, the booster pumps will loose their prime and cease to pump. Additionally, the

amount of vacuum contributed by the pump-out in this scenario only contributes approximately 0.5% of thetotal vacuum rate.

Where,

vs =

k = 1.40

g =

P' =

V = 13.10

Therefore, vs = 1,118 ft/sec

2.53 ft

3.25

Sonic velocity of air, ft/sec

The maximum possible velocity in the Tank's vacuum relief nozzle is:

Specific volume of steam at 14.696 psia =

mean temperature difference between both fluids,oF

For a condensing system, an overall heat transfer coefficient of 250 to 700 Btu/hr-ft2-oF is considered

as very credible. The actual temperature of the rain water could be an estimated 60oF.

If an overall condensing heat transfer coefficient of

For a heat transfer rate heat equation, use:

Heat transfer rate, Btu/hr

Overall heat transfer coefficient, Btu/hr-ft2-oF

Heat transfer surface, ft2

Btu/hr-ft2-oF is used,

There is more than ample cooling rain capability to easily condense all of the incoming 3,000 lb/hr of flash vapor

(1.77 MM Acfd) containing only 7 % volume of non-condensibles.

Vacuum rate inside tank = 10,182,317

Steam condensation rate =

Required nozzle area for sonic velocity =

Quantity of 12" ID open vents required =

Ratio of specific heats for air =

acceleration of gravity, 32.2 ft/sec2

Absolute pressure, psia

Specific volume of air, ft3/lb =

TAUQ D=

VPgkTRgkvs == 144

Page 10 of 13

FileName: 161245513.xls.ms_office

WorkSheet: Condensing Vapor


11/13

Art Montemayor Oil Recovery January 26, 2002

Rev: 0

In order to have safe vessel entry for inspection and repairs of the tank, OSHA requires it be clean of

chemicals. Tanks are normally subjected to cleaning with live steam for this purpose and this procedure

can introduce the hazard of sudden, uncontrolled vacuum developed due to steam condensation during a

rain storm.

Diameter = 50 ft

Height = 32 ft

5,027 ft2

1,991 ft2

7,017 ft2

Where,

Q =

U =

A =

DT =

as very credible. A tropical rain storm at any given time is considered as a design criteria that should be

500

Q = 5.E+08 Btu/hr

506,229 lb/hr

= 253 ton/hr

26.799 ft /lb

ft3/hr

= 226,107 ft3/min

= 3,768 ft3/sec

Where,

vs =

k = 1.40

g =

P' =V = 13.10

Therefore, vs = 1,118 ft/sec

3.37 ft

32 inch diameter

Cylindrical surface area =

Cone top roof surface area =

Total Surface Area =

For a heat transfer rate heat equation, use:

instantaneous cloud burst in the rainy season. The actual rain water temperature could be an estimated 60oF.

strictly observed because of historical, empirical meteorological data. It is very possible to suffer an

Ratio of specific heats for air =

Steam condensation rate =

Specific volume of steam at 14.696 psia =

Volumetric displacement inside tank =

Heat transfer rate, Btu/hr

Overall heat transfer coefficient, Btu/hr-ft2-oF

mean temperature difference between both fluids,oF

For a condensing system, an overall heat transfer coefficient of 250 to 700 Btu/hr-ft2-oF is considered

Heat transfer surface, ft2

If an overall condensing heat transfer coefficient of

Required nozzle area for sonic velocity =

This calculation is for vacuum protection of Crude Oil Storage tanks, T-400 & T-405:

The maximum possible velocity in the Tank's vacuum relief nozzle is:

A nozzle to allow safe operation =

acceleration of gravity, 32.2 ft/sec2

Absolute pressure, psiaSpecific volume of air, ft

3/lb =

Btu/hr-ft2-oF is used,

13,566,429

Sonic velocity of air, ft/sec

TAUQ D=

VPgkTRgkvs == 144


WorkSheet: Steam Out


12/13

TANKS

CLIENT: DOC No 1

JOB: Revision: B of : 1

TANK DATA SHEET

TAG No T-400 Oil Shipping TankGENERAL

SERVICE: Crude Oil VOLUME: Bbls = 470,014 Gallons

TYPE: EMPTY WEIGHT:

INSULATION: Personnel Protection FILLED WITH WATER:

EXTERNAL PAINT: Per Spec 4001 OPERATING WEIGHT:

INTERNAL PAINT: Per Spec 4001 DIMENSIONS:

TRACING: None Diameter 50 feet

Height 32 feet

REF. P&ID:

DESIGN DATACODE: API 650 Latest Edition

RX: Per API 650

HEAT TREATMENT: Per API 650

DESIGN PRESSURE INT.:

CORROSION: 0.125"

AMBIENT TEMP 32-120F

MATERIALSSHELL: A-36

BOTTOM: A-36

ROOF: A-36

PIPES: A53/A106 SMLS

FORGED: A-105

STUDS: A193 Gr B7 Fluorocarbon Coated

NUTS: A194 2H Hvy Hex Nuts Fluorocarbon Coat'd

GASKETS: Flexitallic CG or equal

SUPPORTS:

FITTINGSLADDER: Per API 650 Tables 3-20 and 3-21 LEVEL GAGE

ROOF PROTECTION Per API 650 INSPECTION NOZZLE

CLEANOUT EMERGENCY NOZZLE

NOZZLES

Mark QTY SIZE TYPE Series Locate SERVICEA 1 8" Thief Hatch

B 1 2" RF 150 Gas Blanket

C 1 RF 150 PVSV + Flame Arrestor (Contractor to Size)

D 1 10" RF 150 Inlet

E 1 2" RF LSH

F 1 2" RF 150 TIT

G 1 2" RF 150 LIT

H 1 2" RF 150 LSL

I 1 12" RF 150 Outlet

J 1 4" RF 150 Drain

K 8 2" RF 150 Sample points

M 2 2" RF 150 Level Gauge

N 1 6" RF 150 Foam

MH 1 36"x36" Flush Manway

MH 3 24" FF Manway

Fill Rate 45,000 BPD

Empty Rate 45,000 BPD

NOTES

Platform to be provided as follows: Minimum 4' X 4' Grating Platform at Thief Hatch connected by walkway to

stairs. Construction per API 650 Table 3-19

All nozzle orientations to be defined later

150

11,191

Sheet:

BASIC DATA SHEET

Fixed Cone Roof

AO115-EPF-01-112A1

2 PSIG @ 240 F

MHMHMH

M

MH

MH

A

ACB

D

E

F

G

H

N

I

J

K

M

7/31/2013


13/13

TANKS

CLIENT:DOC No

1JOB: Revision:B of : 1

TANK DATA SHEET

TAG No T-405 Oil Shipping TankGENERAL

SERVICE: Crude Oil Bbls = 470,014 Gallons

TYPE: Fixed Cone Roof EMPTY WEIGHT:

INSULATION: Personnel Protection FILLED WITH WATER:

EXTERNAL PAINT: Per Spec 4001 OPERATING WEIGHT:

INTERNAL PAINT: Per Spec 4001 DIMENSIONS:

TRACING: None Diameter 50

Height 32

REF. P&ID:

DESIGN DATACODE: API 650 Latest Edition

RX: Per API 650

HEAT TREATMENT: Per API 650

DESIGN PRESSURE INT.:

CORROSION: 0.125"

AMBIENT TEMP 32-120F

MATERIALSSHELL: A-36

BOTTOM: A-36

ROOF: A-36

PIPES: A53/A106 SMLS

FORGED: A-105

STUDS: A193 Gr B7 Fluorocarbon Coated

NUTS: A194 2H Hvy Hex Nuts Fluorocarbon Coat'd

GASKETS: Flexitallic CG or equal

SUPPORTS:

FITTINGSLADDER: Per API 650 Tables 3-20 and 3-21 LEVEL GAGE

ROOF PROTECTION Per API 650 INSPECTION NOZZLE

CLEANOUT EMERGENCY NOZZLE

NOZZLES

Mark QTY SIZE TYPE Series Locate SERVICEA 1 8" Thief Hatch

B 1 2" RF 150 Gas Blanket

C 1 RF 150 PVSV + Flame Arrestor (Contractor to Size)

D 1 10" RF 150 Inlet

E 1 2" RF LSH

F 1 2" RF 150 TIT

G 1 2" RF 150 LIT

H 1 2" RF 150 LSL

I 1 12" RF 150 Outlet

J 1 4" RF 150 Drain

K 8 2" RF 150 Sample points

M 2 2" RF 150 Level Gauge

N 1 6" RF 150 Foam

MH 1 36"x36" Flush ManwayMH 3 24" FF Manway

Fill Rate 45,000 BPD

Empty Rate 45,000 BPD

NOTES

Platform to be provided as follows: Minimum 4' X 4' Grating Platform at Thief Hatch connected by walkway to

stairs. Construction per API 650 Table 3-19

All nozzle orientations to be defined later

BASIC DATA SHEET

AO115-EPF-01-112A2

2 PSIG @ 240 F

150

11,191VOLUME:

Sheet:

MH

M

MHMH

M

MH

B CA

D

E

F

G

H

I

J

N

K

M

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Hot Crude Oil Storage.xls