Art Montemayor ProjectCrude Oil Tank

July 29, 2002Rev: 0

Page 1 of 11 FileName: document.xlsWorkSheet: Summary of Results

Summary of Relief Calculations for T-201

The Fire Case is the Controlling Case for Pressure relief; the required relief capacity for this case is 523,215 Scfh. The existing installed pressure relief capacity in the existing 12” Varec Model 2020B1 PVSV is approximately 200,000 Scfh according to Varec Representative in Houston, George Izaguirre.

Existing pressure emergency relief in the existing 24” Varec Model 221P is 750,000 Scfh according to Varec Representative in Houston, George Izaguirre.

Therefore, the existing pressure capacity in T-201 for the new, proposed operating conditions is Scfh. No additional relief capacity is required for T-201 in the manner of a PVSV or an emergency “Fire Hatch” since the present hardware will be sufficient to protect the tank from the worst pressure relief scenario (the Fire Case).

T-201 also has an existing vacuum capacity sufficient for the new, proposed operating conditions.

In the event that steam-out procedures will be used on T-201 in the future, at least 12 ft2 of open roof nozzle area should be available for this tank in order to avoid a vacuum structural failure during a rainstorm while the tank is being steamed-out. This nozzle area can be made up of existing and/or future Fire Hatches as well as any existing roof manways.

Art Montemayor Oil Recovery November 24, 2001Rev: 2(07/24/02)

Page 2 of 11 Electronic FileName: document.xlsWorkSheet: Data Entry

Attachment 1

Tank Padding Calculation SheetData Entry

Stored Material Crude Oil Tank T - 201

Flash Point 350 (Estim.) MAWP in WC 3.50

Boiling Point 360 (Estim.) Max Vacuum 0.50Latent Heat vap. Btu/lb 144.0 (Hexane) Diameter ft 130.0Mol. Wt. 274.0 Max fill ft 40.0

Inflows

Tag Service Line No.Max Head Flow, GPM

Value Units Note 1 Product Transfer to Storage 20"-PL-354-D -157 125 PSIG 1,313 Product Transfer to Storage 12"-PL-756-D -157 50 PSIG 292 Product Transfer to Storage 12"-PL-756-D -157 135 PSIG 729

Total Inflows, gpm 2,333or : Sonic Flow in Pipeor : 135 psior : Other (Attach Method)

Use for Relief (gpm) 2,333

Normal Maximum (gpm) 2,500(Note 3)

Outflows (See Note 1)P-2200 Booster 24"-PL-356-A -157 75 psig 2,000P-2210 Booster 24"-PL-356-A -157 75 psig 2,000P-2220 Booster 24"-PL-356-A -157 75 psig 2,000P-202A Transfer 12"-OP-1910-AA1 -157 100 psig 1,500P-202B Transfer 12"-OP-1910-AA1 -157 100 psig 1,500P-201A Drain 4"-DRG-2900-AA1 -157 65 psig 60P-201B Drain 4"-DRG-2900-AA1 -157 65 psig 60

Total Outflows, gpm 9,120

Notes:

2) The above pump capacities are estimated due to a lack of pump performance curves.3) The "Normal maximum" pump-in rate will be used for the tank relief calculations

oFoF oz/in2

P &ID # 115-01

Pipe Flow at Maximum DP

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

Art Montemayor Oil Recovery November 24, 2001Rev: 4(04/20/08)

Page 3 of 11 Electronic FileName: document.xlsWorkSheet: Design Basis

Attachment 2

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

Stored Material: Crude Oil Tank: T - 201

Flash Point 350 (Estim.) MAWP in. WC 3.5

Boiling Point 360 (Estim.) Max Vacuum 0.5

Latent Heat Vap. Btu/lb 144 (Hexane) Diameter ft 130.0Molecular Wt. 274 Max fill Height ft 40.0

Max fill Volume gal 3,971,616

Inflows, SCFH (Note 3) Wetted Area 12,252.2

Normal Operation 21,429

Relief Scenario 21,429 Fire (Note 2) Unit Heat Input 1,150Required Capacity SCFH 523,214

Outflows, SCFH 73,150Blow-Through From Upstream SCFH 0

Breathing, Note 1 Flashing Feed SCFH 0Out SCFH 56,737In SCFH 64,528 Vacuum Rain Storm Cooling MM Scfh 0.0

Vent Valve set at N.A. in WC Consider this when using an emission vapor control system on the tankRequired SCFH NA Normal max inflow + out breathingselected SCFH NA With vent system Pressure Drop of 9 in WCFail Open SCFH 0 Consider this only if the tank vents to a vacuum source or header

Blanket Gas Feed Valve (set at 7" WC)Required SCFH N. A. Sum of all outflows + in Breathing + failed open vent valve Selected SCFH N. A. 1190 Regulator w/ " trim.Valve Fail Open SCFH N. A. This flowrate assumes the valve's Cv determines the capacity

Pressure and Vacuum Relief CasesInflow (Pressure) SCFH 78,166 Relief Inflow + Out Breathing Fire (Pressure) SCFH 523,214 Fire Case vapors evolved Outflow (Vacuum) SCFH 137,679 sum of outflows + in Breathing

Notes: 1) For Tanks larger than 840,000 gal (20,000 Bbls), refer to API-2000 for breathing requirements.

2)3) The wetted area is equal to the total surface area of the vertical shell to a height of 30 ft (API 2000; Table 3A)

oFoF oz/in2

ft2

BTU/hr-ft2

Fisher Model

Fire Case calculations are according to API Standard 2000, 5th Ed., Section 4.3.3.2.1; Design pressure < 1.0 psig

Art Montemayor Recovery November 24, 2001Rev: 3(04/20/08)

Page 4 of 11 Electronic FileName: document.xlsWorkSheet: Requisition Info

Attachment 3

Storage Tank Pressure/Vacuum Equipment Specifications for ProcurementTANK: T - 201

Conservation VentPressure side set at 1.8 in. W.C. Rated at 2.0 in. W.C.Required SCFH 523,214 zero (if have Vent Valve and Emergency vent) or worst caseSelected Size SCFH each from catalog; total number Total 0

2 1/2Required SCFH 137,679 Outflow CaseSelected Capacity SCFH each from catalog; total number 1 Total 0

Emergency Pressure Relief, Note 1Set at in. W.C. Rated at in. WCRequired SCFH 0 zero (if Con vent has capacity) or Worst case w/o Con VentSelected Size SCFH N. A. each from catalog; total number Total 0

Emergency Vacuum Relief

Set at Rated at in. WCRequired SCFH 0 zero (if Con vent has capacity) or Worst case w/o Con VentSelected Size SCFH each from catalog; total number Total 0

Selected Equipment: Tag Manufacturer Model Size, in

Blanket Gas Regulator N. A. Nitrogen Valve N. A. Conservation Vent PVSV-T20106 Varec 2020B 1 12Emergency Vent (exist.) PSV-T20105 Varec 221P 24Emergency Vent (New)

Notes: 1) A Fire hatch may be required if: cone roof tank does not have a weak roof seam, or if the Conservation Vent

does not have sufficient liquid flow capacity.

This existing tank has the following relief devices installed on it:

200,000 150,000

750,000 0

Total installed Capacity 950,000 150,000

Total Required Capacity 523,214 137,679

Excess Installed Capacity 426,786 12,321

Note: The above Varec Capacities are taken from Varec Vapor Control Product Manual; pages 40 and 101.

The existing, installed Varec relief devices have sufficient pressure and vacuum capacity for the worse cases.No new or additional relief devices are necessary for this storage tank under the calculated conditions.

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

oz/in2

Cv

Rated Pressure Capacity, Scfh

Rated Vacuum Capacity, Scfh

12" Varec Model 2020B1; set @ 1 oz/in2

24" Varec Model 221P; set @ 2 oz/in2

Art Montemayor Oil Recovery November 24, 2001Rev: 3(4/20/08)

Page 5 of 11 Electronic FileName: document.xlsWorkSheet: Case Summaries

Attachment 4

Storage Tank: T - 201Fluid: Crude Oil

Safety Scenario Relief Rates, CFH

Pressure Scenario

Inflow Fire Case Outflow Other

Case Contributions:1 Liquid movement in 21,429 21,429 N.A. N.A.2 Liquid movement out N.A. N.A. N.A. 73,150 N.A.3 Out Breathing (Vapor out) 56,737 N.A. N.A. N.A.4 In Breathing (Vapor In) N.A. 64,528 N.A.5 Fire Exposure 523,214 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. (Note 2) 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 N.A.13 Steam-Out N.A. N.A. N.A. N.A. 46,078,883

Total Volumetric Flow: 78,166 523,214 137,679 46,078,883 0

Controlling Pressure Case Design Capacity = 654,017 cfh (Includes 25% contingency)

Controlling Vacuum Case Design Capacity = 172,098 cfh (Includes 25% contingency)

Air density = 0.0807 32 14.696 psia

Blanket gas density = 0.33425 109 79.7 psiaBlanket gas Molecular Weight = 25.237

Blanket gas density = 0.083877 109 20 psia

Blanket gas specific gravity = 1.0394 109 20 psia

Note 1: The steam-out case is calculated in another Worksheet; relief protection is recommendedin the form of 3 - 30" roof-located manways that are required to be left open while steamingout the tank.

Note 2: No blanket gas is applied on this tank. The maximum operating vacuum rate is set by the maximum pump out of the tank's content.

Vacuum Scenario(Note 1)

Liquid Overflow

Steam-Out (Note 1)

lb/ft3 at oF and

lb/ft3 at oF and

lb/ft3 at oF and

lb/ft3 at oF and

Art Montemayor Storage Tank Pressure ReliefOver-Pressurization Scenario Contributions

November 22, 2001Rev: 2(07/18/2002)

Page 6 of 11 Electronic FileName: document.xlsWorkSheet: OverPressure Scenarios

Consider Event when calculating CASE:

1 2 3 4 5 6 7 8 9 10 11 12No. 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 No2 Liquid Movement Out and Breathing In No Yes No No No Note 2 Note 2 No Note 2 No No No3 Fire Exposure No No Yes No No No No No No No No No4 Pressure Transfer Blow Through No No No Yes No No No No No No No No5 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 No7 Failure of Internal Heating / Cooling Coils No No No No No No No No No No No No8 Failure of Vent Treatment System No No No No No No No No No No No No9 Failure of Utilities (Steam, Nitrogen, air, CWS) No No No No No No No No No No No No

10 Chemical Reaction No No No No No No No No No Note 3 No Note 311 Liquid Overfill No No No No No No No No No No No No12 Flashing Liquid Feed No No No No No No No No No No No No13 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.

Notes:1) This event is when the vent valve feeding tank vapors to a vapor treatment system fails closed.2) Either or both liquid movement events could be applicable depending on the system.3) Consider this event if the fluids involved normally, or potentially, can cause a reaction4) Steam Out is a special case that is handled and calculated independently in another spreadsheet; a properly sized nozzle is usually specified to be left open for this case.

Comments on scenarios for Tank T - 201:

Event No. 4 is not considered a credible scenario since all liquid transfer into tank is done by pumping, not pressure transfer.Event No. 5 is not considered a credible scenario since no blanket gas is fed into the tank.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.Event No. 9 is not considered a credible scenario since no utilities are connected to this tank.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. 11 is not considered a credible scenario since the tank has been designed according to API Standard 2000, 5th Ed.; article 4.2.5.10Event No. 12 is not a possible scenario.

Art Montemayor Storage Tank Pressure Relief May 14, 2002Rev:2(07/18/2002)

Page 7 of 11 FileName: document.xlsWorkSheet: Inflow-Outflow

Determination of Inflows and Outflows for Storage Tanksfor use when calculating Normal and Emergency Venting Requirements

No. Event Inflow / Outflow Calculate Inflow or Outflow by:

1. Liquid Movement in and Breathing Out Inflow

2. Liquid Movement Out and Breathing In Outflow

3. Inflow

4. Pressure Transfer Blow-through Inflow Like Case 1

5. Inert Gas Pad/Purge Regulator Failure Inflow Like Case 1

6. Either or both

7. Failure of Internal Heating/Cooling Coils Either or both

8. Failure of Vent Treatment System Outflow Like case 2

9. Either or both

Chemical Reaction Inflow Like Case 1

Liquid Overfill Inflow This tank is designed according to API Standard 2000, 5th Ed.; article 4.2.5.10

Flashing Liquid Inflow When introducing flashing liquids, always include the flashed vapor in the total relief capacity.

Determine the Maximum flow, at zero head, for each pump that can be lined up to the tank. For sources that are not pump driven, calculate the maximum flow for the flow limiting element. For Control valves, use the largest trim for the valve body and add the capacity of any bypass valves. The total inflow is the sum from all of these sources. The total inflow can be reduced if engineering judgment indicates that it is unlikely that all of the sources will be feeding into the tank simultaneously. The total inflow can also be reduced if the pressure drop in the line(s) between the inlet manifold(s) and tank exceeds the available pressure drop. The available pressure drop is the highest pressure source’s dead head pressure.

Determine the Maximum flow, at zero head, for each pump that can take suction from the tank. The Outflow is the sum of all of these; even installed spare(s).

Exposure to Pool Fire with subsequent tank contents' vaporization

Do not consider inflow for fire case since there is ample time to shutoff the inflow before the fire case fully develops. (see also API-2000 3.4.3.1.4) Do consider the failure of the blanketing gas regulator (if applicable) since these instuments typically fail open and the heat from a fire could cause it to fail.

Failure or loss of Control Heat TransferDevices

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

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

Failure of Utilities (Air, Steam, Cooling Water, N2, etc.)

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

10.

11.

12.

Art Montemayor ProjectOil Storage Tank

June 28, 2002Rev:1(06-9-02)

Page 8 of 11 FileName: document.xlsWorkSheet: Flow Diagram

45,000 Bopd from X 20"-PL-354-D

P-201A20 gpm

P-201B20 gpm

…..… Bopd from Y12"-PL-756-D

T - 201115 oF

12" PVSV -T201061 oz/in2 set press.

24"PSV -T20105

2 oz/in2 set press.

P-202A875 gpm

P-202B875 gpm

P - 22001200 gpm

P - 22201200 gpm

P - 22101200 gpm

To O

il S

hip

ping

P

um

ps

24"-PL-356-A

4"-D

RG

-290

0-

AA

1

12"-

OP

-191

0-A

A1

Art Montemayor ProjectOil Storage Tank

June 28, 2002Rev:1(06-9-02)

Page 9 of 11 FileName: document.xlsWorkSheet: Flow Diagram

To O

il S

hip

ping

P

um

ps

Art Montemayor Eden Yuturi Oil Recovery January 26, 2002Rev: 0

Page 10 of 11 FileName: document.xlsWorkSheet: Steam Out

This calculation is for vacuum protection of Crude Oil Storage tank, T-201: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 = 130 ftHeight = 40 ft

Cylindrical surface area = 16,336

Cone top roof surface area = 13,456

Total Surface Area = 29,792For a heat transfer rate heat equation, use:

Where,Q = Heat transfer rate, Btu/hr

U =

A =

as very credible. A tropical rain storm at any given time is considered as a design criteria that should be strictly observed because of historical, empirical meteorological data. It is very possible to suffer an

If an overall condensing heat transfer coefficient of 400

Q = 2E+09 Btu/hr

Steam condensation rate = 1,719,425 lb/hr= 860 ton/hr

Specific volume of steam at 14.696 psia = 26.799

Volumetric displacement inside tank = 46,078,883

= 767,981

= 12,800

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

Where,

Sonic velocity of air, ft/sec k = Ratio of specific heats for air = 1.40

g =P' = Absolute pressure, psia

V = 13.10

Therefore, 1,118 ft/sec

Required nozzle area for sonic velocity = 11.45

A nozzle to allow safe operation = 46 inch diameter

ft2

ft2

ft2

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

Heat transfer surface, ft2

DT = 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

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

Btu/hr-ft2-oF is used,

ft3/lb

ft3/hr

ft3/min

ft3/sec

vs =

acceleration of gravity, 32.2 ft/sec2

Specific volume of air, ft3/lb =

vs =

ft2

Q=U A ΔT

vs=√k g R T=√k g 144 P' V̄

Art Montemayor Eden Yuturi Oil Recovery January 26, 2002Rev: 0

Page 11 of 11 FileName: document.xlsWorkSheet: Steam Out

3 - 30" Manway nozzles are recommended to be installed on the tank roof