Page 143 - Chemical Process Equipment - Selection and Design

6.8. LIQUID-GAS FLOW IN PIPELINES

. Two-Phase Flow Correlations of Pressure Drop

4. Recommendations
vJpG G (Wmz sec) Correlation
<I000 all Friedel
21000 >I00 Chisholrn-Baroczy
>IO00 400 Lockhart-Martinelli

2. Lockhart-Martinelli Correlation

100

e 10

1
0.01 0.10 1.00 10 100
PARAMETER X

Liquid Gas Subscript C
Turbulent Turbulent tt 20
Viscous Turbulent vt 12
Turbulent Viscous tV 10
Viscous Viscous w 5
3. Chisholm-laroczy Correlation
-
@2 LO - 1 +(yZ- I)[&p"'"(1 -X)(2--n)'2 + x2-"] = (AP/L)/(bB/L),
n = 0.25
y2 = (Ap/L)Go/(Ap/L)Lo
B= 55/G0.', 0 < Y < 9.5
= ~zo/YGO.~, 9.5 < Y < 28
= 15,000/~G0.5, Y>28
x= weight fraction gas
4. Friedel Correlation
3.24FH
q2fo=E+- 3 Fr = Gz/gcDp:p
Fro 045Weo'o '
We = G2D/pTpo
(: 7)
1-x -1
PTP=
0.7
, x=weight fraction gas
llL
1. (P.B. Whalley, cited by G.F. Hewitt, 1982). 2. [Lockhart and Martinelli, Chem. Eng. Prog. 45,
39-48 (1949); Chisholm, Int. J. Heat Mass Transfer 10, 1767-1778 (1967)l. 3. [Chisholm, Int. J.
Heat Mass Transfer 16, 347-348 (1973); Baroczy, Chem. Eng. Prog. Symp. Ser. 62, 217-225
(19691. 4. (Friedel, European Two Phase Flow Group Meeting, Ispra, Italy, Paper €2, 1979, cited
by G.F. Hewitt, 1982).