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Horizontal
Separator with Inlet Nozzle with 90° Elbow (Gas - Oil)
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Process
Calculation
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(
Enter values only in yellow cells)
|
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DATA INPUT
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Gas Standard Volumetric Flow, Qs =
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m³/h
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API Gravity
of Condensate, GsL =
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°
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Standard Pressure, Ps =
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kpa (absolute)
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Specific
Gravity of Gas, GsG =
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Standard Temperature, Ts =
|
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°C
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Liquid Flow
Rate, QL =
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BPD
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TsR =
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°K
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Operating Pressure, Po =
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kpa
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Compressibility
Factor @ ToR (Z) =
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kpa (absolute)
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Operating Temperature, To =
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°C
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Compressibility
Factor @ TsR (Zs) =
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ToR =
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°K
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Fluid Retention time (operation), Tr1 =
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min
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With Mesh
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Fluid Retention time
alarm high, Tr2 =
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min
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Longest side
of a rectangular mesh =
|
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mm
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Fluid Retention time
alarm low, Tr3 =
|
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min
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Mesh thickness =
|
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mm
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With Alarm
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The velocity of the gas in the
outlet nozzle, VGS =
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m/s
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(Considering Maximum Allowable: 18-27 m/s)
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The condensate exit velocity, VLS =
|
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m/s
|
(Considering Maximum Allowable: 1 m/s)
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INTERMEDIATE
CALCULATIONS
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Vessel Longitud tan-tan, L =
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m
|
Assuming a length L seam-to-seam of a container.
The common lengths starting
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Adjust L as necessary. An L/D
ratio between 2.5 and 6 is
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with 2.25 m (7.5 feet) and increase in increments
of 75 cm (2.5 ft).
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satisfactory.
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Vessel Effective Length, Leff =
|
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m
|
It corresponds to the distance between the inlet
nozzle and the gas outlet.
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Relationship L/D =
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P ≤ 1725 kpa
|
use
|
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2.5
|
≤
|
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L
|
<
|
3.0
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As per operating pressure an
initial value of L
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D
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1725 < P ≤
3450 kpa
|
use
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3.0
|
≤
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L
|
<
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4.0
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D
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P > 3450 kpa
|
use
|
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4.0
|
≤
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L
|
≤
|
6.0
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D
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Selected Vessel Diameter, D
=
|
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m
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Selected Vessel Radius, R
=
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m
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Height measured from the bottom
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Cross sectional areas by circular segment
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hLLLL-botton,
h5 =
|
|
m
|
Cross
sectional area between LLLL-botton, A5 =
|
|
m²
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|
The recommended minimum
distance from the low-low level of liquid LLLL to the liquid outlet nozzle is
0.23 m (230 mm)
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hLLL-botton
=
|
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m
|
Cross
sectional area, hLLL-LLLL (emergency) by Volume, A4v =
|
|
m²
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|
hLLL-LLLL (emergency), h4 =
|
|
m
|
Cross
sectional area, hLLL-LLLL (emergency) by h4, A4 =
|
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m²
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A4 ≥ A4v
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hHLL-botton
=
|
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m
|
Cross
sectional area, hHLL-LLL (Operation) by Volume, A3v =
|
|
m²
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hHLL-LLL (operation), h3 =
|
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m
|
Cross
sectional area, hHLL-LLL (Operation) by h3, A3 =
|
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m²
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A3 ≥ A3v
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hHHLL-botton
=
|
|
m
|
Cross
sectional area, hHHLL-HLL (emergency) by Volume, A2v =
|
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m²
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hHHLL-HLL (emergency), h2 =
|
|
m
|
Cross
sectional area, hHHLL-HLL (emergency) by h2, A2 =
|
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m²
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A2 ≥ A2v
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htop-botton
=
|
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m
|
Cross
sectional Gas Area Calculation, AG =
|
|
m²
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|
|
Height the gas in the vessel htop-HHLL, h1 =
|
|
m
|
Gas Area by
h1, A1 =
|
|
m²
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A1
≥ AG
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For horizontal drum
with mesh the minimum vapor space should
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be dimensioned for ho
+ mesh thickness + 300 mm (12 in.)
|
|
Total Area
of Vessel by sum of cross sectional
area, A =
|
|
m²
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or 20% of the
diameter of the drum, whatever is greater.
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Total Cross
Sectional Area of Vessel πR², A =
|
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m²
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For horizontal drum
without mesh the minimum vapor space
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should be dimensioned for 300 mm (12 in.) or
20% of the diameter
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of the drum, whatever is greater.
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Fulfill minimum vapor space in the vessel htop-HHLL, h1 =
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CALCULATIONS
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|
Specific Gravity, GS =
|
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|
|
GS =
|
|
141.5
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°API+131.5
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Liquid
Density, ρL =
|
|
kg/m³
|
|
ρL = GS x ρwater
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Air Density,
ρair =
|
|
kg/m³
|
|
ρair =
|
P x PM
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R x ToR x Z
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|
Gas density: ρG =
|
|
kg/m³
|
|
ρG = GS x ρair
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|
|
Condensate Mass Flow: WL =
|
|
kg/s
|
|
WL =
|
QL
x ρL x 0.0066
|
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|
3600
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|
|
Operation Gas Flow, QG =
|
|
m³/s
|
|
QG =
|
Ps x Qs x ToR x Z
|
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|
P x TsR x Zs x 3600
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|
Gas Mass Flow: WG =
|
|
Kg/s
|
|
WG = QG x ρG
|
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|
Relationship L/D =
|
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|
|
Relationship L/D (NOTE:
minimum allowable L = 2.25 m)
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K =
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K =
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0.122
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if
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2.5
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≤
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L
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<
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4.0
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D
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K =
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0.152
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if
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4.0
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≤
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L
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≤
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6.0
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D
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K =
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0.152
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(L)
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if
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L
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>
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6.0
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LBASE
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D
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(NOTE: maximum allowable K = 0.213)
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Where:
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LBASE
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=
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6 x D
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Gas Speed Calculation, VG =
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m/s
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VG =
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K x
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(
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ρL - ρG
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)
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½
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ρG
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Cross Sectional Gas Area Calculation, AG =
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m²
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AG =
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QG
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VG
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Liquid Flow Rate Calculation, QL =
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m³/s
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QL =
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WL
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ΡL
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Mixture density, ρMIX =
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kg/m³
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ρMIX =
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WL + WG
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QL + QG
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Speed in Nozzle, for the mixture VM =
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m/s
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VMIX =
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80
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(Maximum Allowable: 9
m/s)
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m/s
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(ρMIX)¹ʹ²
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Inlet Nozzle Diameter, dI =
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mm
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dL =
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(
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4(QL+QG)
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)
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½
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Selected Inlet Nozzle Diameter, dI =
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mm
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π x VMIX
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Gas Outlet Nozzle Diameter, dG =
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mm
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dG =
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(
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4QG
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)
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½
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Selected Gas Outlet Nozzle Diameter, dG =
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mm
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π x VGS
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Liquid Outlet Nozzle Diameter, dL =
|
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mm
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dL =
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(
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4QL
|
)
|
½
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Selected Liquid Outlet Nozzle Diameter, dL =
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mm
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π x VLS
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hLLLL-botton,
h5 =
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m
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The minimum
distance from the low-low level of liquid LLLL to the liquid outlet nozzle
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is 0.23 m
(230 mm)
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Wet perimeter angle Ø5 =
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Rad
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Ø5 =
|
2
acos
|
(
|
1
-
|
hLLLL-botton
|
)
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R
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Cross sectional area between hLLLL-botton, A5 =
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m²
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A5 =
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[
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D²
|
(
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Ø5
|
-
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sen
Ø5
|
)
|
]
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8
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Liquid retention volume between hLLL-LLLL, Vr3 =
|
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m³
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Vr3 =
60 x QL x Tr3
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Cross sectional area, hLLL-LLLL (emergency) by Volume, A4v =
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m²
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A4 = Vr3/Leff
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hLLL-botton
=
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m
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Wet perimeter angle Ø4 =
|
|
Rad
|
|
Ø4 =
|
2
acos
|
(
|
1
-
|
hLLL-botton
|
)
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R
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Cross sectional area, hLLL-LLLL (emergency) by h4, A4 =
|
|
m²
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|
A4 =
|
[
|
D²
|
(
|
Ø4
|
-
|
sen
Ø4
|
)
|
]
|
-
|
A5
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8
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Retention
Time, Tr1
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Fluid Retention time (operation), Tr1 =
|
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min.
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|
For Crude ºAPI ≥
40 ® Tr1 = 1½ min
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For Crude 25 < ºAPI
< 40 ®
Tr1 = 3 min
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For Crude ºAPI ≤
25 ® Tr1 = 5 min
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|
Liquid retention volume in Operation, Vr1 =
|
|
m³
|
|
Vr1 =
60 x QL x Tr1
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|
Cross sectional area, hHLL-LLL (Operation) by Volume, A3v =
|
|
m²
|
|
A3 = Vr1/Leff
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|
hHLL-botton
=
|
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m
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|
Wet perimeter angle Ø3 =
|
|
Rad
|
|
Ø3 =
|
2
acos
|
(
|
1
-
|
hHLL-botton
|
)
|
|
|
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R
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|
Cross sectional area, hHLL-LLL (Operation) by h3, A3 =
|
|
m²
|
|
A3 =
|
[
|
D²
|
(
|
Ø3
|
-
|
sen
Ø3
|
)
|
]
|
-
|
A4 - A5
|
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8
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|
Liquid retention volume between hHHLL-HLL, Vr2 =
|
|
m³
|
|
Vr2 =
60 x QL x Tr2
|
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|
|
Cross sectional area, hHHLL-HLL (emergency) by Volume, A2v =
|
|
m²
|
|
A2 = Vr2/Leff
|
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|
|
hHHLL-botton
=
|
|
m
|
|
|
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|
|
Wet perimeter angle Ø2 =
|
|
Rad
|
|
Ø2 =
|
2
acos
|
(
|
1
-
|
hHHLL-botton
|
)
|
|
|
|
|
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|
R
|
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|
|
Cross sectional area, hHHLL-HLL (emergency) by h2, A2 =
|
|
m²
|
|
A2 =
|
[
|
D²
|
(
|
Ø2
|
-
|
sen
Ø2
|
)
|
]
|
-
|
A3 - A4
- A5
|
|
|
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|
8
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|
|
htop-botton
=
|
|
m
|
|
For
horizontal drum with mesh the minimum vapor space should be dimensioned for
ho + mesh thickness + 300 mm (12 in.) or 20% of the diameter of the drum,
whatever is greater.
|
|
|
|
Height the gas in the vessel htop-HHLL, h1 =
|
|
m
|
|
|
|
|
|
|
|
|
For horizontal drum
without mesh the minimum vapor space should be dimensioned for 300 mm (12
in.) or 20% of the diameter of the drum, whatever is greater.
|
|
|
|
|
|
|
|
The minimum distance
between the Mesh and the gas outlet nozzle ho should be adequate to prevent
maldistribution of the flow through the mesh. The minimum distance for this
purpose is presented in the following equation:
|
|
|
|
|
|
|
|
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The min. Dist. between the Mesh & the gas outlet nozzle,
ho =
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mm
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ho =
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FDmesh - dG
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m
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2
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where:
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ho = Minimum
distance from the top of the mesh to the gas outlet nozzle, mm (in.),
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DMesh = Longest side of a rectangular mesh, mm (ft),
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dG = Outlet nozzle diameter mm (in),
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F =Factor whose
value depends on the units used 1 (SI Units) y 12 (US Customary Units).
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Wet perimeter angle Ø1 =
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Rad
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Ø1 =
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2
acos
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(
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1
-
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htop-botton
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)
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R
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Cross sectional area of Gas by h1, A1 =
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m²
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A1 =
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[
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D²
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(
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Ø1
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-
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sen
Ø1
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)
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]
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-
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A2 - A3
- A4 - A5
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8
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