RU2330715C1 - Reactor - Google Patents

Abstract

FIELD: engines and pumps.

SUBSTANCE: invention can be used for intensification of heterogeneous processes at excess pressures accompanied by a significant gas and heat evolution. The reactor shell consists of a cylindrical shell ring, a lower and upper bottoms, and is fitted in a circular support. The lower bottom accommodates a neck, a gas separator connected via a branch pipe to the neck, a sampler and a catalyst inlet pipe, the neck outer surface being attached by stiffening ribs to the circular support. A coiled jacket is arranged below the circular support on the shell ring outer surface. A sprinkler, foam killer and a gate agitator are fitted on a cantilever shaft. The cylindrical shell ring periphery, inside the reactor shell, accommodates six deflector partitions with the lower and upper coiled heat exchangers attached thereto and arranged, respectively, below and above a static agitator attached to the shell ring inner surface.

EFFECT: higher efficiency and higher quality of finished products.

8 cl, 1 dwg

Description

The invention relates to chemical engineering, to the design of reaction apparatuses and can be used to intensify heterogeneous processes at overpressure with high gas and heat generation.

A reactor is known, including a housing, a lid and a bottom, fittings for introducing an initial gas mixture and outputting a target product, a gas-permeable horizontal partition on which a fixed layer of granular catalyst particles is located (Russian patent No. 2283174, B01O 8.02, published on September 10, 2006) .

A known reactor for carrying out heterogeneous processes, comprising a housing consisting of a shell, upper and lower bottoms, a cooling jacket, fittings for the inlet of the main component and the output of the finished product (Application US 2005118088, B01J 8/00, publ. 02.06.2006).

A reactor is known that allows heterogeneous exothermic synthesis, consisting of a vertical cylindrical body, spherical caps and bottoms, fittings for introducing the initial gas mixture and outputting the target product, cold gas dispensers arranged horizontally at different levels in the reactor and dividing the continuous catalyst layer into conventional ones located layers (Japanese Application N58-47214, CL C07C 31/04). The mixture of hot and cold gas takes place in hollow chambers having a vertical section in the form of a rhombus and placed around the cold gas distributors.

A known reactor for conducting heterogeneous exothermic synthesis (US Pat. No. 3,480,407, class C07C 31/04) having a vertical cylindrical body consisting of a shell with upper and lower bottoms, a fitting for introducing the initial gas mixture and outputting the target product. Between the gas-permeable partitions with the catalyst layers there is a mixing chamber. Mixed hot and cold gas flows enter the mixing chamber through openings made in the side wall of the housing. A hot stream is formed in the catalyst bed, and a cold stream comes from the inlet portions of the feed gas mixture through the distribution means. To provide additional mixing of the gas flows, the chamber is equipped with vertically arranged blades, creating peripheral turbulent flows in it. The exit from the mixing chamber is made in the form of an opening in the lower horizontal partition in the central part of the reactor.

The closest is a reactor for carrying out processes in heterogeneous environments, containing a casing with a heat exchange jacket, a cantilever shaft with a mixing device, baffles, a coil of the nozzle of the input of the main component and the output of the finished product (Russian patent No. 2132726, B01J 8/10, publ. 10.07. 1999)

This reactor is adopted as a prototype of the invention.

In the known designs of reactors for this purpose, there are a number of the following disadvantages:

- instability of the process;

- the formation in the upper part of the reaction zone of a foam gas layer (ASG) with a concentration of catalyst in it;

- insufficient rate of formation of the final product due to large losses of reagents in the flue gas;

- funnel formation in the liquid phase;

- insufficient mixing of the reagents, the formation of stagnant zones in which the catalyst accumulates;

- poor dispersion of the gas in the liquid;

- gas separation at the shaft of the mixing device;

- insufficient heat removal of the exothermic reaction.

The objective of the invention is to increase the productivity and quality of the product resulting from the synthesis, due to improvements in design.

The problem is achieved in that in a reactor containing a casing with a heat-exchange coil jacket, a cantilever shaft, a mixing device, baffles, an input fitting for the main component and an outlet for the finished product, the casing consists of a cylindrical shell, upper and lower bottoms, and is fixed in an annular support, on the upper bottom there is a neck, a gas separator connected by a nozzle to the neck, a sampler and a catalyst inlet pipe, and the outer surface of the neck is rigidly connected by ribs with an annular support, a coil jacket is fixed below the annular support on the outer surface of the shell, a sprinkler, defoamer and stand mixer are fixed on the cantilever shaft, six reflective walls are installed around the perimeter of the cylindrical shell, on which the upper and lower coil heat exchangers are located, respectively lower and above a static mixing device mounted on the inner surface of the shell.

Additionally, the inlet of the main component inlet and the outlet of the finished product are installed diametrically opposite in the cylindrical shell, in the area of the stand mixer.

Additionally, the sprayer, which provides irrigation of the inner part of the body, has a plate shape with vertical ribs located on the periphery.

Additionally, the upper and lower bottoms are elliptical in shape.

Additionally, the antifoam consists of a set of horizontal ribs and vertical ribs located at an angle of 30 ° to the axis of the cantilever shaft.

Additionally, the cantilever shaft through a flange connection is connected to the output shaft of the drive of the mixing device, the support of which has a cylindrical shape with a flange and is mounted on the neck.

Additionally, the gas separator is connected by a nozzle to the neck, and a fitting for introducing a liquid reagent is installed in the upper part of the nozzle.

Additionally, the static mixing device consists of six propeller-type blades uniformly spaced in the diametrical section of the reactor and installed at an angle of 30 ° to the horizontal plane to meet the flow of the reaction mixture supplied through the gas distribution device.

The invention is illustrated in the drawing.

Schematic diagram of the reactor

The reactor includes a vertical casing 1, consisting of a cylindrical shell 2, the upper bottom 3 and the lower bottom 4, having an elliptical shape. The housing 1 is fixed in an annular support 5. On the outer surface of the shell 2, below the annular support 5, a heat-exchange coil jacket 6 is fixed, consisting of series-connected and parallel-working sections. A neck 7 is installed on the upper bottom 3, and the outer surface of the neck is connected to the annular support 5 by stiffening ribs 8. Inside the housing 1 there is a mixing device consisting of a cantilever shaft 9, on which a sprayer 10 is mounted, providing irrigation of the inner part of the housing and having a plate shape with located along the periphery of the vertical ribs, defoamer 11, consisting of a set of horizontal ribs and vertical ribs located at an angle of 30 ° to the axis of the cantilever shaft 9, at the end of the shaft A turbulent device in the form of a cage mixer 12 has been updated. The cantilever shaft 9 is connected via a flange connection 13 to the output shaft 14 of the stirring device drive 15, the support 16 of which has a cylindrical shape with a flange, and is mounted on the neck 7. Inlet fitting 17 of the main component A and fitting 18 the output of the finished product is installed diametrically opposite in the cylindrical shell 2, in the area of the cage mixer 12.

On the flange 19 of the support 16, a fitting 20 is installed for introducing a liquid reagent - component B. An end seal 22 is installed on the inner flange 21 of the support 16, filled with a barrier fluid and ensuring the tightness of the output shaft 14.

On the lower bottom 4 of the housing 1 is installed a gas distribution device 23, made in the form of a bubbler with a nozzle input 24 of the reaction mixture. In the upper bottom 3 of the housing 1, a gas separator 25 is installed, connected by a nozzle 26 with a neck 7, a catalyst inlet tube 27, a sampler 28, which serves to control the composition of the working mixture, manhole 29, a fitting 30 is installed in the upper part of the nozzle 26 for introducing component B. On the inside the surface of the shell 2 of the housing 1 is fixed static mixing device 31, consisting of a support 32 with a bearing located in the support, allowing operation in aggressive environments, and six propeller-type blades uniformly located in the diametric section reactor and installed at an angle of 30 ° to the horizontal plane opposite the flow of the reaction mixture supplied through the gas distribution device 23. Six reflective walls 33 are installed along the perimeter of the cylindrical shell 2 inside the reactor vessel 1, which facilitate mixing of the mixture in the peripheral part of the working zone. Inside the housing 1 above the mixing device 31 is located the upper coil heat exchanger 34, below the lower coil heat exchanger 35, mounted on the reflective partitions 33.

The reactor operates as follows. Component A is fed to the inlet of the reactor through the nozzle 17 in the shell, and the reaction mixture is supplied from below through a gas distribution device 23 to the specified reactor filling volume. The design of the gas distribution device 23 provides a uniform distribution of incoming gases in the reaction volume in the area of the stand mixer 12. To start and put the reactor into operation, depending on the reaction temperature, a frequency-control converter (not shown) is switched on with a stirrer 15. The torque from the output shaft 14 of the actuator 15 is transmitted to the cantilever shaft 12 of the mixing device by means of a flange connection 13. Thus, the foam is included in the operation Itel 11 and the stand mixer 12. The mixture of components in the reactor begins to mix intensively due to the rotation of the stand mixer 12 and the effective effect of the static mixing device 31. The propeller-type blades installed at an angle to the horizontal plane contribute to intensive mixing and uniform distribution of the catalyst previously supplied through the input tube 27. The installation distances of the stand mixer 12, the static mixing device 31 and the antifoam 11 are determined empirically.

After the reactor enters the mode, the frequency-control converter is turned off and the predetermined number of revolutions is supported by the drive 15 of the mixing device. The rotation of the defoamer 11, installed at the optimum height, prevents the formation of a foam-gas layer, flotation of catalyst particles and the entrainment of components from the reactor. When component B is fed to the catalyst, an exothermic synthesis reaction occurs. To maintain the specified heat transfer mode, the upper 34 and lower 35 coil heat exchangers are used, which are installed on the reflective partitions 33. The reflective partitions 33 facilitate additional turbulization of the working mixture in the peripheral zone of the heat exchanger installation and on the cooled reactor wall, which significantly increases the heat transfer coefficients of the medium. The cross section and the number of turns of both the cooling coil heat exchangers 34 and 35, and the heat exchange coil jacket 6 also provide high heat transfer coefficients on the part of the coolant, and, as a result, heat transfer coefficients sufficient to remove heat from the exothermic reaction. Gases released during the synthesis process are discharged through a pipe 26 connected to the neck of the reactor 7 and sent to the gas separator 25. During its operation, a stream is created that entrain the entrained catalyst particles and directs them down to the working area. The gas freed from solid particles penetrates the gas separator body 25 and is discharged from the reactor. The component B enters the apparatus through two fittings 20 and 30 located in the upper part of the reactor. Component B, which facilitates the reaction on the catalyst, enters both the middle zone of the apparatus together with the returning particles of the solid phase and the zone of operation of the defoamer 11 through the hole in the neck 7. This creates additional conditions for the synthesis reaction to take place in the upper zone. Through the nozzle 20, located on the flange 19 of the support 16 of the reactor neck, component B is fed to the sprayer 10. The spray stream, washing the catalyst from the inner surface of the reactor, returns with solid particles to the upper reaction zone, which also intensifies the process due to the additional reagent and catalyst. The finished product is discharged from the reactor through the outlet fitting 18.

The use of a static mixing device provides intensive mixing and uniform distribution of the catalyst suspension in the volume of the liquid phase.

The use of a cage mixer and antifoam, installed at a certain height, eliminates funnel formation in the liquid phase. This reduces the entrainment of gases and catalyst, which increases the conversion of the reactants, the reaction rate, the quality of the product and increases the productivity of the reactor.

The supply of component B to the sprayer increases the safety of the reaction, intensifies the synthesis process and promotes the return of the catalyst to the working zone.

The use of a flange connection of the output shaft of the drive and the console shaft of the mixer increases the reliability of the drive.

The use of a gas separator virtually eliminates the entrainment of the catalyst from the apparatus and, in addition, ensures the introduction of the component into the middle part of the reaction zone to intensify the process.

The use of a frequency-control converter provides a smooth start and stop of the reactor and reduces the time to exit to the mode.

The coil jacket, consisting of parallel sections, provides sufficient heat dissipation from the reactor wall due to the high heat transfer coefficient.

Coil heat exchangers located inside the housing have an enlarged heat transfer surface and a high heat transfer coefficient from the walls to the coolant.

The baffles to which the heat exchangers are attached increase the rigidity of the reactor structure.

Claims (8)

1. The reactor, comprising a housing with a heat-exchange coil jacket, a cantilever shaft, a mixing device, baffles, an input fitting for the main component and an outlet for the finished product, a gas distribution device, characterized in that the housing, consisting of a cylindrical shell, upper and lower bottoms, is fixed in annular support, on the upper bottom there is a neck, a gas separator connected by a nozzle to the neck, a sampler and a catalyst inlet pipe, the outer surface of the neck being connected stiffening ribs with an annular support, a coil jacket is fixed below the annular support on the outer surface of the shell, a spray gun, antifoam and stand mixer are fixed on the cantilever shaft, six reflective walls are installed around the perimeter of the cylindrical shell on which the upper and lower coil heat exchangers are mounted, respectively lower and higher than a static mixing device mounted on the inner surface of the shell. 2. The reactor according to claim 1, characterized in that the main component inlet fitting and the finished product outlet fitting are installed diametrically opposite in the cylindrical shell, in the area of the stand mixer. 3. The reactor according to claim 1, characterized in that the sprayer, providing irrigation of the inner part of the housing, has a plate shape with vertical ribs located on the periphery. 4. The reactor according to claim 1, characterized in that the upper and lower bottoms are elliptical in shape. 5. The reactor according to claim 1, characterized in that the antifoam consists of a set of horizontal ribs and vertical ribs located at an angle of 30 ° to the axis of the cantilever shaft. 6. The reactor according to claim 1, characterized in that the cantilever shaft through a flange connection is connected to the output shaft of the drive of the mixing device, the support of which has a cylindrical shape with a flange, and is mounted on the neck. 7. The reactor according to claim 1, characterized in that in the upper part of the pipe connecting the gas separator with the neck, a fitting is installed for introducing a liquid reagent. 8. The reactor according to claim 1, characterized in that the static mixing device consists of six propeller-type blades uniformly spaced in the diametrical section of the reactor and installed at an angle of 30 ° to the horizontal plane to meet the flow of the reaction mixture supplied through a gas distribution device.