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Vertical
Separator with Flush Inlet Nozzles or 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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TsK =
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°K
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Operating Pressure, Po =
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kPa
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Compressibility
Factor @ Tok (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 @ Tsk (Zs) =
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ToK =
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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 (emergency), Tr2 =
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min
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With Alarms
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Fluid Retention time
alarm low (emergency), Tr3 =
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min
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The velocity of the gas in the
outlet nozzle, VGN =
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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, VLN =
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m/s
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(Considering Maximum Allowable: 1 m/s)
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CALCULATIONS
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Specific Gravity, GS =
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GS =
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141,5
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°API+131.5
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Liquid
Density, ρL =
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kg/m³
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ρL = GS x ρwater
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Air Density,
ρair =
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Kg/m³
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ρair =
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P x PM
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R x T x Z
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Gas density: ρG =
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Kg/m³
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ρG = GS
x ρair
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Condensate Mass Flow: WL =
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Kg/s
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WL =
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QL
x ρL x 0.0066
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3600
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Gas Flow Rate, QG =
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m³/s
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QG =
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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 =
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Kg/s
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WG = QG
x ρG
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Relationship WL / WG
=
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K =
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K = 0.107 if
WL/WG <
0.1
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K = 0.076 if
0.1 ≤ WL/WG ≤ 1
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K = 0.061 if
WL/WG >
1
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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 Area Calculation, A =
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m²
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A =
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QG
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VG
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Vessel Inner Diameter Calculation, Dc =
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m
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Dc =
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(
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4 x A
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½
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π
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Selected Vessel Inner Diameter, D =
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m
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Definitive Cross Sectional Area, A
=
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m²
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A =
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D² x π
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4
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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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dI =
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(
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4(QL+QG)
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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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Height between the inlet nozzle’s top
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and the drum’s top tangent line, h1
=
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m
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Height
between the inlet nozzle’s top and the drum’s top
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tangent line,
hnoozle-tang (h1):
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-
Perpendicular entry and no mesh: 920 mm (Approx 3 ft) or
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0.5D, whichever is
greater.
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-
Perpendicular entry and with a mesh: 400 mm (16 in) or
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0.15D,
whichever is greater + 150 mm (6 in) + 610 mm (24 in)
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or 0.5D, whichever is
greater.
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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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Fluid Retention Volume (operation), Vr1 =
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m³
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Vr1 =
60 x QL x Tr1
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Height the liquid in the vessel (operation), h4 =
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m
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h4 =
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Vr1
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A
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Height the liquid in the vessel hdp-HHLL, h2 =
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m
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In the case of vertical drums with perpendicular entry:
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Consideging minimun of 0.3D, hdp-HHLL, h2 =
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m
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hNAAL-boq = dI
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Fluid Retention Volume alarm high (emergency), Vr2 =
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m³
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Vr2 =
60 x QL x Tr2
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Height the liquid in the vessel alarm high (emergency), h3
=
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m
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h3 =
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Vr2
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A
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Fluid Retention Volume alarm low (emergency), Vr3 =
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m³
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Vr3 =
60 x QL x Tr3
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Height the liquid in the vessel alarm low (emergency), h5
=
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m
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h5 =
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Vr3
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A
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Height the liquid in the vessel hLLLL-botton, h6 =
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m
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The
minimum distance (h6) from the low-low level of liquid
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LLLL to the liquid
outlet nozzle is 230 mm minimum.
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Vessel Length, L =
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m
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L = h1 + dp + h2 + h3 + h4 + h5 + h6
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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 VGN
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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
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)
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½
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Selected Liquid Outlet Nozzle Diameter, dL =
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mm
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π x VLN
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Check
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Estimate the total
length seam to seam of the vessel considering economic relations L/D of the
vessel with the margin from 2.5 to 6.
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Verify that the final
computed L / D ratio falls in this range. If L is too low, arbitrarily
provide more time of liquid retention if L is too high,
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follow a horizontal
design. Whenever possible, the lengths and diameters should be adjusted to
produce sizes that match the standard
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designs of the equipment suppliers.
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LMIN =
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m
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LMIN = 2.5 x D
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LMAX =
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m
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LMAX = 6 x D
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Vessel Length, L =
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m
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