SU889086A1 - Reactor - Google Patents

Description

(54) REACTOR

The invention relates to chemical reactor designs and can be used in polymerization processes involving gaseous and liquid reagents and a catalyst. . A device is known to continuously conduct reactions between a gaseous product and a liquid in a flow tube reactor with a vertical arrangement of tubes filled with a nozzle and coolant circulating in the annular space. The movement of gas and liquid in the tubes occurs in a bottom-up direction. To obtain a uniform The distribution of the gas line over all the tubes of the apparatus at the inlet of each tube is established. a nozzle or a porous plate so as to obtain a pressure drop of at least half the hydrostatic pressure of the liquid in the tubes of the apparatus. There are two types of apparatus, differing in the way the liquid is distributed through the tubes. One method is to use liquid suction. each tube apparatus using; A special tube of smaller diameter immersed at one end into a liquid supplied to the lower casing of the apparatus. Another method is to distribute the liquid from the bath located in the upper casing of the apparatus, for which a tube of smaller diameter is placed in each tube with a nozzle, through which the fluid enters the lower part of the nozzle to the gas inlet I. Also known is a column for countercurrent contact, inside of which packages of plates with curved upper edges are vertically mounted. The plates are equally spaced from each other. The irrigating fluid is supplied through the nozzle and is evenly distributed over the surface of the plates by means of a perforated plate. Steam is discharged through openings in the choke. The liquid carried off by steam is discharged through another fitting. The column is tested at a diameter of 350 mm and a height of 6 and on a mixture of methanol and water with a distance between the plates of 7.12 and 24 mm. It is found that the number of plates, equivalent to 1 m of the height of the plates is 0.5-1.0. Steam velocity is 3-5 times Exceeds steam velocity in a reactor with a nozzle. Separating action Columns with irrigated plates over a wide range are practically independent of changes in productivity. The advantage of the column is low hydraulic resistance, due to which these columns are particularly suitable for gas-phase. reactions under vacuum. In this case, the steam velocity up to I7 m / s can be achieved. On the basis of theoretical considerations, a method for calculating reaction columns with irrigated plates under laminar and turbulent regimes is proposed, which is compared with the results of experiments. The large separating action under the laminar regime, predicted by the theory, was not confirmed by experiments. With an increase in the steam velocity, the experimental values of the hydraulic resistance amount to 60% of the calculated ones. Reducing the distance between the plates from 24 to 12 mm causes an increase in the separation capacity of the column 2. A disadvantage of the known devices is the discontinuity of the contacting cycles along with the high consumption and overrun of the zinc catalyst and the energy intensity of the processes. The closest to the proposed design and the effect achieved is a reactor for gas-liquid chemical reactions using a liquid catalyst, containing a vertical body, plane-parallel plates installed in the body, a liquid catalyst distributor made in the form of a collector with nozzles and located in the upper part of the body, and the inlet and outlet connections of the reagents, the catalyst and the finished product. The disadvantage of the known reactor is that the film Lastin is distributed unevenly as a result of the vertical arrangement of the plates. 6 which, in turn, leads to an increase in the thickness of the liquid film in the lower part of the plates, an increase in thermal resistance and a decrease in the reaction temperature. In addition, there are catalyst losses and significant heat consumption. The aim of the invention is to intensify the process by ensuring the separation of the catalyst from the finished product, its circulation and use for heating the body of an exothermic polymerization reaction. The goal is achieved by the fact that the reactor is equipped with curved partitions fixed on one of the walls of the casing, forming receiving pockets, brackets fixed on the opposite wall of the casing, wire bags parallelly placed above the plates and forming with them flat channels mi for feeding semi-duct, placed on brackets and restrictive bars connecting the ends of the wire bags with pipes, and the plates and wire bags are installed Inclined obliquely between the brackets and curved partitions, with flat channels connecting the slots of the tubes with the receiving pockets. FIG. 1 image; Ken reactor, OBDIJ type, longitudinal section; Fig.2 shows the technological scheme of the installation in which the proposed reactor is used. A reactor for conducting gas-liquid chemical reactions using a liquid catalyst consists of a vertical body 1, plane-parallel plates 2, installed in a housing, a liquid catalyst distributor, made in the form of a collector 3 with a pipe 4 and nozzles 3 and located in the upper part of the body, fittings 6-14 input and output of reagents, catalyst and finished product, mounted on one of the walls of the body of the curved partitions 15, forming the receiving pockets 16, brackets 17, mounted on against bying wall of the housing, the wire packet 18, parallel arranged above the plates 2 and forming them flat channels 19, pipes 20 are formed in the longitudinal slots 21 for supplying w

intermediate product, placed on the brackets 17, and restrictive bars 22, connecting the ends of the wire bags 18 to the pipes 20.

The plates 2 and the wire bags 18 are mounted obliquely between the brackets I7 and the curved partitions 15. The flat channels 19 connect the slots 21 of the pipes 20 with the receiving pockets 1 6.

The reactor operates as follows.

The reactants entering into the reaction flow into chamber 23 through fitting 6 and 7, distribution manifold 3, pipeline 4 and dispense nozzles 5 /. The same chamber 23 enters the form of vapors of the second, the reactant with catalyst vapors from the last two separators 24 and 25 and due to its condensation heat the liquid. Heating of the liquid also occurs from the bottom of chamber 23, which is the upper part of chamber 26. In chamber 23, the main reaction takes place between the reactants in the presence of a liquid catalyst.

For greater intensity of the entire reaction process, vacuum is maintained in chamber 23 — vacuum by pump 27, which deaerates all reagents. The product from the chamber 23 through the nozzle 8, the pipe 28, the collector 29 and the flow regulator 30 enters the pipes 20, at the exit of which the restricting strips 22 create a uniform film of bluntness flowing along the inclined surface of the plates 2. These plates 2 are heated by steam from chambers 26, as a result of which it evaporates from the liquid film. The resulting liquid catalyst vapor passes through the bag 18, being cleaned of liquid droplets that flow into the pockets 16. The vapor condenses on the upper plate 2 and the resulting condensate is held by adhesion and surface tension, but flows under the force of gravity along the plate 2 into the pocket 16, from which it is withdrawn through nozzles 9 into the separator 24. In the separator 24, the product boils up as it is connected to the chamber 26 located above, and in which the pressure is lower than the product entering the separator 24. The pressure value in the next chamber 26 is maintained by a pressure regulator 31.

89086,6

The liquid on the bottom plate 2 evaporates, resulting in an additional reaction of the components and an increase in the concentration of the liquid catalyst 5. The catalyst concentrate through the nozzle 10 into the separator

25, where vapors of the secondary boiling of a separator 24 are separated from it.

О The liquid outlet from the separators 24 and 25 is limited by a level regulator 32, after which the liquid enters the following separators 24 and 25. Steam is also extracted from this liquid,

5 which enters the next chamber

26. After the last separator 24 by the pump 33, the clean product pumps. C into a tank (not shown) or for further processing.

20 After the last separator 25, the concentrated catalyst is pumped by pump 33 into chamber 23 through filter cyclone 34 through pipe 35 and fitting 7. Secondary steam from the last separators 24 and 25 enters chamber 23, where it gives off heat and condensate from the mixture of components.

Heating steam for the reactor enters the heating chamber 36 through the fitting 1I and as a result of condensation, heat is transferred to the plate 2 of the lower chamber 26. The condensate from the chamber-36 leaves through the fitting 2 to the condensate collector (not shown). The heat of the heating pa, pa is used in the reactor many times, for example 16 times in chambers 23 and 26. Economic efficiency is expressed in the processability of the process and in increasing the productivity of the reactor, in reducing heat consumption and

catalyst for the process of synthesis and polymerization of organic intermediates.

45

Claims (2)

Invention Formula A reactor for conducting gas-liquid chemical reactions using a liquid catalyst, containing a vertical case, plane-parallel plates installed in the case, a liquid catalyst distributor, made in the form of a manifold with nozzles and located in the upper part of the case, and fittings for input and output of reagents, catalyst and of the finished product, in order to intensify the process by ensuring the separation of the catalyst from the finished product, its circulation and use for After heating the heat of the exothermic polymerization reaction, it is equipped with curved perforations fixed on one of the housing walls, forming receiving pockets, brackets fixed on the opposite wall of the housing, .wire packets parallel to the plates and forming flat channels with them, filled with longitudinal peaks in them for supplying semi-finished products placed on brackets and restrictive bars connecting the ends of wire bags with pipes, and the plates and wire bags are installed obliquely between the brackets and curved partitions, with flat channels connecting the slots of the pipes with receiving pockets. Sources of information taken into account in the examination 1. The patent of Germany 1207924, cl. .2d, 2/01, 07/14/1966. 2 .. Technik, 1955, v. 7, No. 11-, p. 638-647. 3 .. prumysl, 1956, t. 8, No. 11, p. 581-583. 35 jj  H IS g te I Rig.2