An Experimental and Theoretical £ Investigation of Annular Steam ...

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When the steady state was achieved, the following dimensionless
heat balances were made for test purposes:
reg
h 2~ h 3
n^-hg
n.ex. m n c —h,
s 5 6
where m (kg/s) is the (primary) suction rate and m (kg/s) is
P
s
lated by means of
the (secondary) cooling rate.
The heat balance on the regenerator, HB , is theoretically
unity when water only is sucked off the test section.
The heat balance on the heat exchanger, HB, , becomes
theoretically unity when all the steam in the suction mixture
is condensed in the regenerator. This is supposed to be fulfilled
when the values the difference of HB. T - 2 was T, always is greater within than the 50 range C. In 0.95-1.05.
these cases,
The steam flow in the suction mixture, m , is then calcum
g = ((h 5 -h 6 )m s +(h 7 -h 8 ) m p - (h 2 ~h 4 )m p )/r ev . (3.6)
If all the steam is condensed in the regenerator, it is
seen from eq. (3.5) that
m
m
9
= -£- (h 7 -h 8 -(h 2 -h 3 )).
ev
(3.7)
Due to the smaller number of parameters in the latter
equation, m was determined by eq. (3.7) when the difference
T_-T 3 was greater than 50°C.
The liquid flowrate in the mixture, m,, was now determined
by
m, = m -in . (3.8)
1 p g
For each adjustment of the total suction rate, three measurements
of m and ra, were carried out. The mean values were then
9 1
plotted in the suction diagram where iru/m is shown versus
x
out
.-m
g
/m. The total suction rate was then varied until a
sufficient number of points was obtained to draw a suction
curve. A typical example is shown in fig. 3.9.