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
7/22/2019 Hot Crude Oil Storage.xls
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
7/22/2019 Hot Crude Oil Storage.xls
3/13
Art Montemayor Oil Recovery November 24, 2001
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
7/22/2019 Hot Crude Oil Storage.xls
4/13
Art Montemayor Oil Recovery November 24, 2001
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
each from catalog; total number
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
each from catalog; total number
Outflow Case
each from catalog; total number
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
Electronic FileName: 161245513.xls.ms_office
WorkSheet: Requisition Info
7/22/2019 Hot Crude Oil Storage.xls
5/13
Art Montemayor Oil Recovery November 24, 2001
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
Electronic FileName: 161245513.xls.ms_office
WorkSheet: Case Summaries
7/22/2019 Hot Crude Oil Storage.xls
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
7/22/2019 Hot Crude Oil Storage.xls
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
Page 7 of 13FileName: 161245513.xls.ms_office
WorkSheet: Inflow-Outflow
7/22/2019 Hot Crude Oil Storage.xls
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.
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.
e case 2
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.
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
Page 8 of 13FileName: 161245513.xls.ms_office
WorkSheet: Inflow-Outflow
7/22/2019 Hot Crude Oil Storage.xls
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
7/22/2019 Hot Crude Oil Storage.xls
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
7/22/2019 Hot Crude Oil Storage.xls
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
Page 11 of 13FileName: 161245513.xls.ms_office
WorkSheet: Steam Out
7/22/2019 Hot Crude Oil Storage.xls
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
7/22/2019 Hot Crude Oil Storage.xls
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
Top Related