ANALYSIS OF THE HEAT EXCHANGE PROCESS IN A TUBULAR FILM ABSORBOR DURING SULPHATION OF MIXTURES OF ORGANIC SUBSTANCES

Abstract

The article states that the production of surfactants consists of the following stages: catalytic oxidation of sulfur dioxide, sulfation, neutralization and purification of gaseous emissions. The sulfation step is the main stage at which high-quality intermediates can be obtained.
 It has been shown that tubular film absorbers are used for the sulfation process, which create mild conditions for the exothermic reaction due to efficient heat dissipation. This makes it possible to obtain high-quality surfactants both in terms of the degree of sulfation, and in terms of light products.
 It is stated that a tubular film absorber with a descending phase flow is a vertical structure with two flows: a liquid phase film and a gas-air flow, ie. a two-phase system.
 The presence of two phases changes not only the forms of motion of such systems, but also their nature, as the interaction between the phases has a decisive influence. In contrast to single-phase flows, new forces are manifested at the interface of two-phase flows - forces of interphase surface tension, which affect both the process of mass transfer and the process of heat transfer.
 It is shown that in periodicals there is little data on the impact on the process of heat transfer temperatures and consumption of starting reagents.
 Such studies will make it possible to create a more modern design of industrial tubular film absorber.
 The data of the analysis on the choice of temperatures and costs of the used reagents are given. A deeper analysis of heat transfer processes was performed by the method of mathematical modeling.
 A simplified mathematical model is presented, which allows to analyze the heat transfer process along the length of the absorber. A program for calculating the process of sulfation of a mixture of organic substances in a tubular film absorber using the application package MathLab.
 The results of mathematical modeling for three velocities of gas flow: 16 m/s, 20 m/s, 24 m/s, which were recommended in the analysis of the costs of starting reagents.
 It is shown that the main amount of reaction heat is transferred to the cooling water along the entire length of the absorber.