Russian Journal of Applied Chemistry, 2009, Vol. 82, No. 4, pp. 719−722.
Pleiades Publishing, Ltd., 2009.
Original Russian Text
A.V. Dzheranin, 2008, published in Khimicheskaya Promyshlennost’, 2008, Vol. 85, No. 7, pp. 359−363.
PROCESSES AND DEVICES
OF CHEMICAL MANUFACTURES
Temperature Proﬁ le in a Displacement Reactor
A. V. Dzheranin
Biisk Technological Institute, Department of Altai State Technical University, Biisk, Russia
Received August 1, 2008
Abstract—Results of a mathematical simulation of the heat and mass exchange in the displacement reactor are
Parameters of a heterogeneous liquid-phase process
and the temperature proﬁ le in the displacement reactor
 were deﬁ ned for 5 types of a non-linear change
in a channel temperature h with a continuous and
discontinuous phase (Fig. 1). We conducted calculations
assuming division of 2 mm drops of the dispersed phase
in an upper section of the reactor moved from a center
to a periphery in the channel narrowing over the height
along with the continuous medium while calculations for
a bottom section of the reactor (at the continuous ﬂ ow
movement from the periphery to the center in the channel
widenning along the height) were performed assuming
a fusion of the drops of the dispersed phase.
An increase in a number of the drops of the dispersed
phase (of an interfacial area) in the upper section of the
partially provided a signiﬁ cant efﬁ ciency of
transformation (73–78%) of an initial constituent of the
dispersed phase for a short residence time in the reactor
channel. Also a temperature increase of the medium
in the upper reactor section for the ﬁ rst type to 71°С
was detected, and for the other 4 types the medium
temperature of the uppers section of the reactor was in
a range of 54–59°С.
Therefore similarly to  using a model of  we
compute parameters of heterogeneous liquid-phase
process with the fast chemical transformation on the
more interfacial area due to feeding the dispersed phase
of 1 mm drops in the reactor. The dispersed phase and the
continuous medium are fed the channel in amount of
−0.35, and 1.3 kg/s, respectively. The temperature proﬁ le
in the reactor channels is computed by an equation of the
heat balance for the channel section of a length dR with
a heat transfer surface dF (Fig. 1), and solving the Cauchy
limitng-value problem analogously to .
We varied non-linearly the height of the channel with
the continuous and dispersed phases for 3 types (1, 2, 3)
of a construction likewise to : h = aR, and for 2 types
(4, 4**) linearly h = a + b R (see Fig. 1, and the table).
Coefﬁ cients a, and b of the channel height h denote the
hannel narrowing in the upper section, and extension in
the bottom section (along the continuous ﬂ ow).
Fig. 1. A scheme of the displacement reactor: (1) the channel
with dispersed phase G
and continuous medium G
an external upper G
and bottom G
channels with a cooling
agent, (3) the internal channel G
with the cooling agent.