RU2344876C1 - Nozzle falling film reactor for conduction of chemical processes - Google Patents

Abstract

FIELD: engines and pumps.

SUBSTANCE: reactor comprises cylindrical body that contains tapered cover and bottom, nozzles for reagents supply and discharge of reaction products, three-position sprayer of initial fluid reagents and film-forming elements, at that tapered cover and bottom are arranged with angles at the tops of 90-120° and 30-60° accordingly, reactor body contains diaphragm that separates it into two sections, at that pipe is installed coaxially to body in diaphragm opening, on top of the pipe expander is installed with vertical perforated tubes, and at the pipe bottom packet of vertical blades is installed, which are fixed on support plate at angle α to radial direction equal to 45-50°, rectangular nozzle for reagents supply with three-position sprayer is installed tangentially in bottom section of body, at that top edge of tangential nozzle has 1.5-2.0-turn helical tray fixed to it and specified pipe, installed with clearance δ relative to body wall, equal to 2-4 mm, in radial direction tray is inclined at angle θ, equal to 6-10°, and spiral film-forming elements are vertically installed on helical tray at equal distance from each other, having clearance δ with downstream turn of tray.

EFFECT: provides intensification of heat and mass exchange processes, required speed of gaseous chloride hydrogen desorption, higher efficiency, neutralisation of hazardous gaseous production wastes.

3 cl, 5 dwg

Description

The invention relates to equipment for carrying out heat and mass transfer chemical processes, in particular hydrolysis, esterification, acidolysis of organosilicon monomers and other reactions proceeding with the release of toxic gaseous products, and can be used in the chemical, food and pharmaceutical industries.

Known capacitive apparatus equipped with a mechanical stirrer to obtain organosilicon oligomers (Khananashvili L.M. Chemistry and technology of organoelement monomers and polymers. M: Chemistry. 1998, p.197).

However, as a rule, devices of this type have large volumes, which complicates the necessary heat and mass transfer with the removal of by-product gaseous products and the desorption of hydrogen chloride from the reaction mass due to the relatively low interface.

In order to intensify the contact of the reagents with each other and accelerate the desorption of hydrogen chloride at the initial stage of the process, hydrolysers equipped with a pumping unit that creates a circulation loop are used (Khananashvili L.M. Chemistry and technology of organoelement monomers and polymers. M .: Chemistry. 1998, p. .199).

The use of such devices leads to the formation of by-products due to prolonged contact of the reaction products with gaseous hydrogen chloride and concentrated hydrochloric acid.

Known apparatus of the nozzle type for gas purification, containing a cylindrical body, means for loading and unloading, a shock-jet nozzle with a nozzle for irrigated solution, a reflector in the form of a hollow spherical segment (AS USSR No. 1207485, IPC B01J 19/26, B05B 1/26, 1986).

The main disadvantage of the described device is the low yield of the target products, as well as the lack of a system for controlling the ratio of components, high losses of reaction products through the suction channels of gaseous hydrogen chloride and ineffective heat and mass transfer and desorption of hydrogen chloride.

The closest in technical essence to the proposed invention is a nozzle film-type reactor for carrying out chemical processes, containing a cylindrical body, including a conical cover and a bottom, nozzles for introducing reagents and outputting reaction products, a three-position atomizer of the initial liquid reagents and film-forming elements (RU 2236899 C1, 27.09 .2004).

The disadvantages of this invention include the entrainment of a certain part of an expensive liquid along with HCl gas and the large dimensions of the apparatus when using viscous liquids.

The technical result of the invention is to ensure the intensification of heat and mass transfer processes, the necessary rate of desorption of gaseous hydrogen chloride, increasing productivity, as well as neutralizing harmful gaseous waste products.

The technical result is provided by a reactor that contains a cylindrical body, including a conical cover and bottom, nozzles for introducing reagents and output of reaction products, a three-position atomizer of the initial liquid reagents and film-forming elements, while the conical cover and bottom are made with angles at vertices of 90-120 ° and 30 -60 °, respectively, in the reactor vessel there is a diaphragm dividing it into two sections, and a pipe is placed coaxially to the case in the diaphragm hole, on top of which an expander is installed from the vertical GOVERNMENTAL perforated tubes and pipes placed at the bottom packet vertical blades fixed on the base plate at an angle α to the radial direction, equal to 45-50 °. A rectangular nozzle for introducing reagents with a three-position atomizer placed in it is tangentially mounted in the lower section of the housing, and a 1.5-2.0-turn screw tray attached to the specified pipe connected with a gap δ relative to the housing wall is connected to the upper edge of the tangential nozzle equal to 2-4 mm, in the radial direction, the tray is inclined at an angle θ equal to 6-10 °, and spiral film-forming elements are installed vertically at an equal distance from each other on the screw tray, having the second turn of the tray clearance δ.

The ratio of the height of the lower section of the cylindrical body to its diameter H: D is 1.5: 2.0, and the ratio of the diameter of the pipe to the diameter of the body d: D is 0.4-0.6: 1.

The length of the coaxial pipe (L) in the lower section of the reactor is determined by the formula

where K = 6-8 is a coefficient characterizing the influence of the ratio H: D on the length L, a smaller value of K corresponds to lower values of H: D and vice versa;

R is the radius of the reactor vessel;

r is the radius of the coaxial pipe;

γ is the angle at the apex of the conical bottom.

The invention is illustrated by drawings, where Fig. 1 is a general view of a reactor, Fig. 2 is a general view of a three-position atomizer of liquid components, and Figs. 3, 4, and 5 are cross-sections and sections for explaining the structures of assemblies.

The apparatus (figure 1) contains a cylindrical body 1, a conical cover 2 and a bottom 3 with nozzles 4 and 5, respectively. The diaphragm 6 divides the housing 1 into two sections, in the lower section a rectangular pipe 7 is tangentially installed with a three-position pneumatic atomizer (nozzle) of liquid materials 8, the channels of which serve to supply the liquid reaction products 9, water 10 and hot nitrogen 11. In the hole of the diaphragm 6, a pipe 12 is placed coaxially with the apparatus body, the upper end of which is equipped with an expander 13 and vertical perforated tubes 14, and a packet 15 with blades 23 that are attached to the support plate those 16, along the symmetry axis of the support plate has a tapered cone 17. On the tube 12 is mounted a screw 19 with vertical tray spiral film-forming elements 20. The upper section of the housing has nozzles for supplying water 21 and output 22 hydrochloric acid.

The reactor operates as follows. Organosilicon monomer and water are respectively supplied through channels 9 and 10 of a three-position pneumatic atomizer of liquid materials 8, water is directed at a high speed to the outlet channel of atomizer 24, injecting organosilicon monomer, the two streams are mixed and form a reaction mixture in which the hydrolysis process begins in diffusion mode. The resulting mixture is ejected at high speed into the nozzle 7 and sprayed into small drops, with the maximum contact of the reacting components with each other.

At the same time, heated nitrogen gas is supplied through channel 11 of a three-position pneumatic atomizer under a pressure of 3-12 atm. Since the channel is circular and is inclined with respect to the axis of symmetry, the nitrogen flow forms a conical gas funnel in front of the outlet of the atomizer with an angle at apex β through which the atomized reaction mixture passes. At the moment the reagents exit the outlet channel of the nebulizer, droplets of liquid components fall into a conical nitrogen funnel and, leaving it, fly apart along diverging trajectories. In the collision of nitrogen molecules with liquid droplets, they are crushed into even smaller particles, while intensive physical and chemical interactions take place and the hydrolysis process is carried out already in a kinetic mode with a high speed to the end.

The atomized mixture of reaction products with gaseous components through the pipe 7 enters the zone of the location of the spiral film-forming elements 20, where the flow is divided into thin layers that begin to move in a spiral. Under the influence of centrifugal forces, the trajectory of the droplets of the reaction products changes, they are pressed against the walls of the reactor vessel, the coaxial pipe and the film-forming elements, forming a film of liquid products on them, flowing from the walls of the film-forming elements to the tray 19. From the tray, the liquid products are sent in a continuous stream through the gaps through the gaps to the walls of the reactor vessel. In the process of the film regime, the chemical interactions and the purification of liquid products from gas inclusions - deaeration, including the desorption of hydrogen chloride, are simultaneously completed. The gas components of the process, freed from liquid droplets, fall into the free volume of the lower section of the apparatus, enclosed between the bottom 3 and the coaxial pipe 12. The conical shape of the bottom of the apparatus enhances the vortex movement of the gas flow, centrifugal forces press this flow against the walls of the bottom, where the most small drops of liquid from a gas stream. From the bottom of the apparatus, the gas flow rises up to the coaxial pipe 12 with the package of blades 15 installed on it, where it breaks up on the conical fairing 17 and enters the interscapular spaces, changing the direction of movement by 90 °. The final purification of the gas stream from the liquid reaction products on the walls of the coaxial pipe occurs. The purified gas stream rises up the pipe into the expander 13 and in its perforated tubes 14 is bubbled through a layer of water, which comes from the pipe 21. When dissolved in water, hydrogen chloride is converted into hydrochloric acid, which is removed from the apparatus through the pipe 22, and the purified nitrogen through pipe 4 goes into the atmosphere. Liquid reaction products are discharged through pipe 5.

Claims (3)

1. The nozzle reactor of the film type for carrying out chemical processes, comprising a cylindrical body including a conical cover and a bottom, nozzles for introducing reagents and output of reaction products, a three-position atomizer of the initial liquid reagents and film-forming elements, characterized in that the conical cover and bottom are made with angles at peaks 90-120 ° and 30-60 °, respectively, in the reactor vessel there is a diaphragm dividing it into two sections, and a pipe is placed coaxially to the body in the opening of the diaphragm, on top of which a reamer with vertical perforated tubes was installed, and a packet of vertical blades mounted on the base plate at an angle α to a radial direction of 45-50 ° was placed at the bottom of the tube, a rectangular pipe for introducing reagents with a three-position sprayer placed in it was tangentially installed moreover, with the upper edge of the tangential pipe is connected 1.5-2.0-x spiral screw tray attached to the specified pipe, installed with a gap δ relative to the housing wall, equal to 2-4 mm, in a radial m toward the tray is tilted at an angle θ, equal to 6-10 °, and equidistant from each other on the tray vertically mounted screw spiral film-forming elements having a coil from the lower tray δ gap. 2. The reactor according to claim 1, characterized in that the ratio of the height of the lower section of the cylindrical body to its diameter H: D is 1.5: 2.0. 3. The reactor according to claim 1, characterized in that the ratio of the diameter of the pipe to the diameter of the casing d: D is 0.4-0.6: 1.

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