of light petroleum products, including the naphtha from the T-1 tower, was 53.5%, and the gas yield
was 2%.
Steam feed to the tower included the following: 1% to the diesel fuel stripping tower and 1.44% to the
bottom of the T-2 tower. The absolute pressure in the tower was 2.2 kgf/cm 2. The vertical temperature
distribution in the tower was as follows: feedstock at inlet to tower 360~ tower top 140~ takeoff of kerosene
from tower 200~ takeoff of diesel fuel 298~ tower bottom 340~ PTsO temperatures (takeoff/feedback) as
follows: PTsO-1 154/70~ PTsO-middle 228/70~ PTsO-2 252/86~ Calculated from the operating test
data were the mass and heat balances, reflux ratio, number of theoretical trays, and hydrodynamic charac-
teristics of tray operation. The percentage vapor flashed off at the inlet of the topped crude to the tower was
determined by a procedure set forth in [4]. In calculating the hydrodynamic indices, use was made of equations
given in [5, 6]. The basic parameters of multicomponent distillation, i.e., the minimum operating reflux ratio,
the optimum reflux ratio, and the number of theoretical trays for the sections of the tower, were determined
by a procedure set forth in [7]. Special features involved in calculating the basic parameters of distillation in
a complex tower for crude oil separation are given in 本文来自辣$文(论"文?网，
毕业论文 www.751com.cn 加7位QQ324~9114找原文[8].
The composition of the vapor feed (composition of the load) for calculation of each section was assumed
on the basis of the mass balance of the corresponding section of the tower and was determined from the equation
of the working line,
. R x~o (1)
where R is the reflux ratio in the lower part of the section; Xiw and XiD are the concentrations of the i-th
component in the reflux and rectified product from the section, respectively,
In calculating the bottom sections (kerosene and diesel fuel), it was assumed that the composition of the
vapor leaving the section is equal to the composition of the rectified product from these sections.
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