Description Usage Arguments Value References See Also Examples
View source: R/MukherjeeBrill.R
Return the dimensionless groups proposed by Duns & Ros (1963):
NLv
: Liquid velocity number
NGv
: Gas velocity number
Nd
: Pipe diameter number
NL
: Liquid viscosity number
NGvSM
: Slug/(Annular Mist) transition
NGvBS
: Bubble/Slug transition (Downflow)
NLvBS_up
: Bubble/Slug transition (Upflow)
NLvST
: Stratified (Downflow)
1 2 | l_dlns_MB(vsG, vsL, ID, densityG, densityL,
viscosityG, viscosityL, surfaceTension, angle)
|
vsG |
Superficial velocity of gas |
vsL |
Superficial velocity of liquid |
ID |
Pipe internal diameter |
densityG |
Density of gas |
densityL |
Density of liquid |
viscosityG |
Visosity of gas |
viscosityL |
Visosity of liquid |
surfaceTension |
Surface tension |
angle |
Pipe angle in radian (0 is horizontal flow) |
Data frame including dimensionless numbers (NLv
, NGv
, Nd
, NL
,
NGvSM
, NLvBS
, NGvBS_up
, and NLvST
) and input values (vsG
,
vsL
, D
, densityG
, densityL
, viscosityG
, viscosityL
,
surfaceTension
, and angle
)
Mukherjee, H., and J. P. Brill. 1985. Empirical Equations to Predict Flow Patterns in Two-Phase Inclined Flow. International Journal of Multiphase Flow 11 (3)
Duns, H. and Ros N. C. J. 1963. Vertical flow of gas and liquid mixtures in wells. In: 6th World Petroleum Congress
1 2 3 4 5 6 7 8 9 10 11 12 13 14 | # This example is from Brill and Mukherjee (1999)
# "Multiphase Flow in Wells" p.21, p.46 (Example 3.2 and 4.8)
vsG <- 3.86 * 0.3048 # 3.86 ft/s
vsL <- 3.97 * 0.3048 # 3.97 ft/s
ID <- 6 * 0.0254 # 6 inch
densityG <- 5.88 * 16.01845 # 5.88 lbm/ft3 - (1 lbm/ft3 = 16.01845 kg/m3)
densityL <- 47.61 * 16.01845 # 47.61 lbm/ft3 - (1 lbm/ft3 = 16.01845 kg/m3)
viscosityG <- 0.016 / 1000 # 0.016 cp
viscosityL <- 0.97 / 1000 # 0.970 cp
surfaceTension <- 8.41 / 1000 # 8.41 dynes/cm
angle <- pi/2 # 90 deg (upward)
# NLv=11.87, NGv=11.54, NGvSM=350.8, NLvBS_up=18.40, NL=0.0118
l_dlns_MB(vsG, vsL, ID, densityG, densityL, viscosityG, viscosityL, surfaceTension, angle)
|
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