Reactor for dehydrogenation of paraffinic hydrocarbons c3-c5

FIELD: petrochemical processes.

SUBSTANCE: invention concerns reactor with fluidized bed of fine catalyst, which reactor contains upright cylindrical body, sectioning grids with their free area increasing along the height of reactor, connecting pipes for supplying feedstock and evacuating contact gas, and receiving and withdrawing recycled catalyst, and cyclones with dust-removing risers. More specifically, upper grid has free area larger than 60 and lesser than 90% of the body section, ends of connecting pipes receiving recycled catalyst and ends of dust-removing risers are disposed above upper grid and below fluidized bed.

EFFECT: increased output of reactor, improved performance of dehydrogenation (increased yield of olefins and reduced consumption of catalyst), and improved environmental condition.

1 dwg

 

The invention relates to the field of petrochemicals, in particular for reactors for dehydrogenation of paraffin hydrocarbons With3-C5in the corresponding olefinic hydrocarbons, used to obtain the basic monomers of synthetic rubber, as well as in the production of polypropylene, methyltrichlorosilane ether and other

Known reactor for dehydrogenation of paraffin hydrocarbons with a fluidized bed of fine-grained catalyst comprising a vertical cylindrical housing and partitioning the grid, set the height of the fluidized bed ("Industry synthetic rubber", Moscow, Tsniiteneftehim, 1968, No. 2, p.8, Rkirilow, Anwesen "Joint dehydrogenation of butane and isopentane in a fluidized bed of fine-grained catalyst").

However, in this reactor partitioning of the lattice have the same free cross-section that defines a non-uniform distribution of catalyst in sections of the reactor and the low rates of dehydrogenation outputs of olefins on missing and decomposed raw materials.

The closest in technical essence is a reactor for dehydrogenation of paraffin hydrocarbons With3-C5fluidized bed of fine-grained catalyst comprising a vertical cylindrical housing, the partitioning of the lattice with increasing height of the reactor free széchenyi is m, connections input materials and output contact of the gas input and output of the circulating catalyst and cyclones with filespacename risers (RF Patent No. 2156161 on 31.03.1999. Reactor for dehydrogenation of paraffin hydrocarbons With3-C5). In the specified reactor lower grille has a free section that constitutes 10-30% of the cross-section of the casing, and the upper 20-60%. The ends of the pipes entering the circulating catalyst and pulespusti riser cyclones are located in the surface area of the fluidized bed (nadsloevom space of the reactor).

The design is known reactor eliminates the disadvantages of the above analogue, but in turn characterized by low productivity and relatively low rates of dehydrogenation.

Improving the performance of known reactor by increasing the diameter leads to irrational increase of metal and problems characteristic of the transition to large scale reactors and associated with increased non-uniformity of the flow distribution of the gas and the circulating catalyst, and the temperature in the cross section of the reactor.

Improving the performance of the reactor by increasing the gas velocity in the cross section also encounters significant difficulties. In the conditions of the upper grid of known reactor, nl is skih to the mode zahlebyvayas, with minimal mixing (recirculation) of the catalyst on the grill worsen conditions input streams circulating catalyst from the regenerator and caught in the cyclone catalyst dust in the volume of the fluidized bed below the top of the lattice, which prevents the involvement of these threads in circulation through the reaction volume. Arriving in the upper part of the fluidized bed above the upper grate the catalyst is subjected to the secondary ash in netslave space of the reactor. The specified leads to increased removal of catalyst from the reactor through cyclones to increase its production losses, as well as to increase the temperature in nadsloevom space of the reactor and thus to undesired transformations of hydrocarbons in the volume of this space. In addition, when increasing the gas velocity in the known reactor in the upper part of the fluidized bed there is a significant thermal non-uniformity associated with the increase of temperature difference on the upper grille, which also leads to the decrease of dehydrogenation.

These disadvantages of the known reactor-related options in the upper grid, are exacerbated by the input surface of the fluidized bed (netslave space) superheated circulating catalyst from the regenerator and the cooled catalyst from the cyclones.

For the of ACA of the present invention is to increase the efficiency of the reactor by increasing its productivity and performance dehydrogenation.

To solve this problem is proposed reactor for dehydrogenation of paraffin hydrocarbons With3-C5fluidized bed of fine-grained catalyst comprising a vertical cylindrical housing, the partitioning of the lattice with increasing height of the reactor free cross-section, the outlet of input materials and output contact of the gas input and output of the circulating catalyst and cyclones with filespacename struts, in which the upper grille has a free cross-section of more than 60 and less than 90% of the cross-section of the housing and the ends of the pipe entering the circulating catalyst and pulespusti riser cyclones are installed above the top bars below the level of the fluidized bed.

In the proposed reactor increase the free cross section of the upper grid in combination with depth in the boiling layer entry points of the circulating catalyst and return captured by the cyclones of the catalyst can improve the conditions for inclusion of the flows of catalyst circulation through the volume of the fluidized bed by increasing the mixing of the catalyst in the upper part of the layer (in the area of the upper grid of the reactor) and the introduction of flow of the catalyst directly in the zone of the fluidized bed intensive mixing of the catalyst. This reduces the secondary ash in netslave space reactor coming into the upper part of pasego layer flow of a catalyst and as a consequence there is a possibility of increasing the productivity of the reactor by increasing the gas velocity in the cross section. At the same time is aligned to the profile of temperature change along the reactor, increase performance dehydrogenation (output olefins on missing and decomposed raw material). Reduced loss of catalyst in the production and improving the ecology of dehydrogenation processes.

The drawing shows a diagram of the proposed reactor.

The reactor has a housing 1, piping and connections for input 2 and output 3 of the circulating catalyst, raw inlet 4 and the contact strip 5. The reactor also contains a distributor of raw materials 6. Fluidized bed of catalyst in the reactor 7 is divided into sections partitioning grating (lower grille 8, the upper bars 9, which is located in the high temperature zone of the fluidized bed 10). The reactor has a Stripping zone 11 with the supply line in an inert gas 12, the separation zone (netslave space reactor) 13, which are cyclones with 14 filespacename struts 15. The pipeline input superheated catalyst from the regenerator to the reactor 2 has a nozzle 16 with the discharge ends 17. Pilsuskyi risers cyclones 15 have outlet ends 18.

The reactor operates as follows.

The vaporized paraffin hydrocarbons (raw materials) are fed into the reactor through the pipeline and the pipe 4 through the valve 6. In the Stripping zone 11 and the pipe 12 is supplied inert gas to otpa the ku from hydrocarbon waste from the reactor catalyst. In the lower part of the reactor (between the distributor and the bottom bars) pairs of raw materials are mixed with the rising of the riser gases bog and then climb boiling layer of catalyst, passing successively partitioning the lattice, then getting into the separation zone 13. Caught in the cyclone 14 and chilled in the separating zone, the catalyst is returned to the risers 15 through the outlet ends 18 in the high-temperature part of the fluidized bed above the upper partitioning bars 9.

Application of heat to provide the endothermic dehydrogenation reaction is circulating through the regenerator catalyst. Regenerated and heated catalyst coming from the regenerator through the pipeline 2 and the nozzle 16 through the discharge ends 17 in the high-temperature part of the fluidized bed above the upper partitioning grating 9, and then passes a section of a reactor with a fluidized bed of catalyst prototechno rising pairs of raw materials, and gradually cools down during the endothermic dehydrogenation reaction, and through the Stripping zone 11 through the pipeline and the pipe 3 in splenorenal and restored the form is returned to the regenerator by burning coke oxidation and heating. Thus is formed the temperature profile of the reactor with the temperature increase from the first (lower) sections of the reactor, located between what aspredinidae and lower bars, to its high temperature zone above the upper partitioning grid.

Contact gas dehydrogenation after removing dust in the separating zone and the cyclone 14 through the pipeline 5 is directed to the cooling and extracting the obtained olefinic hydrocarbons.

Thus, in the proposed reactor due to more efficient organization of its work is achieved by increasing the productivity of the reactor, the improvement in dehydrogenation (increase outputs of olefins on missing and decomposed raw materials, reduces the consumption of catalyst), also improves the ecology of dehydrogenation processes in connection with the reduction of environmental pollution gone with the catalyst.

Reactor for dehydrogenation of paraffin hydrocarbons With3-C5fluidized bed of fine-grained catalyst comprising a vertical cylindrical housing, the partitioning of the lattice with increasing height of the reactor free cross-section, the outlet of input materials and output contact of the gas input and output of the circulating catalyst and cyclones with filespacename struts, characterized in that the upper grille has a free cross-section of more than 60 and less than 90% of the cross-section of the casing, the ends of the pipes entering the circulating catalyst and pulespusti riser cyclones are installed above the top bars below, Ural branch of the nya fluidized bed.



 

Same patents:

FIELD: petrochemical processes.

SUBSTANCE: feed stream is passed with admixed oxygen and diluent through catalyst bed at 400-500°C and constant flow rate 50 mL/min, said catalyst being catalytic system for heterogeneous reactions and representing geometrically structured system including microfibers of high-silica fibrous carrier, which is characterized by presence in IR absorption band of hydroxyl groups with wave number ν=3620-3650 cm-1 and half-width 65-75 cm-1. The carrier has specific surface as measured according to BET method from heat desorption of argon SAr=0.5-30 m2/g, surface area as measured by alkali titration method SNa=5-150 m2/g at ratio SNa/SAr=5-50, and at least one active element, whose principal portion is composed in the form of charged either metallic, or bimetallic clusters characterized in UV-vis diffuse reflection spectrum by specific bands in the region 34000-42000 cm-1 and ratio of integral intensity of band attributed to charged either metallic, or bimetallic clusters to integral intensity of band belonging to, respectively, either metallic, or bimetallic particles is not less than 1.0.

EFFECT: increased choice of oxidative dehydrogenation catalysts.

4 cl, 5 ex

FIELD: petrochemical processes.

SUBSTANCE: branched olefins are obtained via dehydrogenation of isoparaffin composition containing 0.5% or less quaternary aliphatic carbon atoms in presence of suitable catalyst. Isoparaffin composition is prepared via hydrocracking and hydroisomerization of paraffin wax and contains paraffins with 7 to 18 carbon atoms, these paraffins or at least a part of them are branched with average number of branches between 0.5 and 2.5 per paraffin molecule, the branches including methyl and optionally ethyl ones. Original paraffin wax is prepared using Fischer-Tropsch reaction. Resulting branched olefins are characterized by content of quaternary aliphatic structures 0.5% or less. Branched aromatic hydrocarbon and compositions of branched olefins, branched aromatic hydrocarbon, and branched alkylarenesulfonates are also disclosed.

EFFECT: improved quality characteristics of target products.

10 cl, 19 ex

FIELD: petrochemical processes.

SUBSTANCE: branched olefins are obtained via catalytic dehydration of isoparaffin composition including 0.5% or less of quaternary aliphatic carbon atoms. This isoparaffin composition comprises paraffins with number of carbons within a range of 7 to 35, said paraffins or at least a part thereof being branched with average number of branches from 0.7 to 2.5 and said branches including methyl and optionally ethyl branches. Indicated isoparaffin composition with is obtained via hydrocracking and hydroisomerization of wax. Thus obtained branched olefins contain 0.5% or less of quaternary aliphatic carbon atoms.

EFFECT: upgraded quality characteristics of desired products.

8 cl, 4 tbl, 11 ex

FIELD: industrial organic synthesis.

SUBSTANCE: ethylbenzene blend obtained through blending fresh ethylbenzene and recycled ethylbenzene with styrene content not above 0.1 wt % is subjected to catalytic dehydrogenation in presence of water steam at feed-to-steam weight ratio 1:2, temperature 600°C, ethylbenzene blend supply space velocity 0.5-1.0 h-1, and reactor pressure maintained within a range of 45 to 80 kPa absolute. Multistep rectification gives rectified styrene with concentration of desired product at least 99.8% and phenylacetylene impurity level not higher than 0.01 wt %. Recycled ethylbenzene is blended with fresh ethylbenzene and resulting ethylbenzene blend containing no more than 0.1 wt % styrene is supplied to dehydrogenation unit.

EFFECT: increased ethylbenzene-to-styrene conversion, improved process selectivity, and reduced level of phenylacetylene in commercial product.

5 tbl

FIELD: petrochemical industry; methods of production of styrene.

SUBSTANCE: the invention is pertaining to the field of petrochemical industry, in particular, to the method of production of styrene. The invention provides for dehydrogenation of the ethylbenzene charge gained after mixing of the fresh ethylbenzene with the recycled ethylbenzene on the ferrioxide catalytic agent at presence of the steam at the mass ratio of the raw to the steam of no less than 1:2, at the temperature of 580-640°С and the volumetric speed of feeding of the ethylbenzene charge of 0.23-0.45 m3/h. The hydrocarbon condensate (the product of the dehydrogenation) containing styrene, the unreacted ethylbenzene, the by-products including the phenyl acetylene impurity before the stage of the rectification is hydrogenated using the palladium-containing catalytic agents at the temperature of 20-30°С, the volumetric speed of 4.5-5.0 m3/h-1 and at the volumetric ratio of the hydrogen : raw - 35-45. The technical result of the invention is the increased purity of the produced styrene without reduction of productivity of the whole process of the marketable styrene.

EFFECT: the invention ensures the increased purity of the produced styrene without reduction of productivity of the whole process of the marketable styrene.

1 tbl, 8 ex

FIELD: organic chemistry, chemical technology, catalysts.

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EFFECT: improved and valuable properties of catalyst.

12 cl, 2 tbl

FIELD: hydrogenation-dehydrogenation catalysts.

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22 cl, 2 tbl, 16 ex

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EFFECT: improved method for isomerization.

4 cl, 2 tbl, 2 ex

FIELD: chemistry of aromatic compounds, chemical technology.

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61 cl, 2 tbl, 2 dwg, 2 ex

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EFFECT: improved preparing method.

1 tbl, 6 ex

FIELD: chemical industry; devices for production of the synthesis gas.

SUBSTANCE: the invention is pertaining to the radial type device for realization of oxidation of the gaseous hydrocarbon fuels with the help of the catalytic agent and may be used for production of the synthesis gas. The radial type device for production synthesis gas contains the gas-distribution perforated tube 3 and the catalytic agent 4. The catalytic agent is made in the form of the annular heat-conducting dispensing catalytic plates and the heat-conducting separators with the grooves alternating among themselves with formation of channels for the gaseous streams running and connected among themselves. On the both sides of the separator 6 there are grooves 7 made in the form of the evolvent from the center to the periphery. The annular plates of the catalytic agent are mounted perpendicularly to the axis of the shafts of the gas-distribution perforated tube 3. Inside of the gas-distribution perforated tube 3 there is the starting system, which consists of the mixer 1 with the ignition plug 2 or the electric heating component. The invention presents the compact and effective device.

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6 cl, 3 dwg

Reactor // 2284217

FIELD: petrochemical industry; devices for hydrocarbons processing.

SUBSTANCE: the invention is pertaining to the field of petrochemical industry, to the devices used for hydrocarbons processing, in particular, to the reactor containing the vertically elongated reaction chamber, having, at least, one reaction layer and the reactor internal device. At that the reactor internal device contains the essentially horizontal lower supporting grating and, at least, one distributor made in the form of the distribution plate and the means for distribution of the cooling liquid medium. The distribution device is arranged above and at a distance from the lower supporting grating and is connected with it by means of the vertical elongated supports. The lower supporting grating rests on the upper surface of the reaction layer. Besides, the invention is pertaining to the usage of such reactor in the method of the hydrocarbons processing. The technical result of the invention is arrangement of the reactor internal device at the desirable vertical level of the reaction chamber.

EFFECT: the invention ensures arrangement of the reactor internal device at the desirable vertical level of the reaction chamber.

12 cl, 4 dwg

FIELD: chemical industry; methods and installations for treatment of the discharge gases in the processes of desulphurization.

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EFFECT: the invention ensures reduction of the output of the hydrogen sulfide and-or the sulfur dioxide.

23 cl, 3 dwg

FIELD: chemical engineering; production of reactors for catalytic synthesis.

SUBSTANCE: the invention is pertaining to the field of chemical engineering, predominantly to reactors of catalytic synthesis. The horizontal multi-shelved catalytic reactor consists of a load-bearing plate, a high-pressure cylindrical body with a cover, which may be transported along the axis of the catalytic unit. The reactor has the typical component and the design of components of the catalytic unit, which consists of the sealed cylindrical catalytic containers, the load-bearing support frame and the module-type heat-exchange devices. The load-bearing support frame represents a crosswise section beam cantileverly fixed on the load-bearing support plate. The vertical plane of symmetry of the frame coincides with the longitudinal axis of the high-pressure body, and on the shelves there are catalytic containers installed in two parallel rows. The frame is cantileverly fixed to the load-bearing plate, through which all inlets and outlets are carried out. The plate is upright mounted on the horizontal foundation and the high-pressure body is joined with it. In the module heat-exchange devices there are tracts for passage of the reactionary gases and the heat-transfer medium. The invention ensures improved conditions of the reactor operation, reduction of its overall dimensions and the mass, simplification of the process of manufacture.

EFFECT: the invention ensures improved conditions of the reactor operation, reduction of its overall dimensions and the mass, simplification of the process of manufacture.

2 cl, 6 dwg

FIELD: chemical industry; equipment for synthesis of hydrocarbons.

SUBSTANCE: the invention is pertaining to chemical industry, in particular, to the horizontal reactor for synthesis of hydrocarbons according to Fisher-Tropsh method. The offered reactor consists of the single-type design coaxial horizontal reactive sections. Each section is mounted on a wheeled trolley with adjustable supports and incorporates a casing, a fixed in it through adapters catalytic box with a built-in heat exchanger, through which the heat transfer medium is compulsorily pumped over. The catalytic box is made in the form of a package assembly of the same type catalytic modules is sectional with usage of the fastening strainers and tightening gaskets. The catalytic module is assembled with usage of welding from longitudinal or transversal in respect to the longitudinal axis sections, the square-type flat soldered on corrugations or ribs double walled panels with the general depth of 5-15 mm, at the thickness of walls of 1 - 2 mm, at the height of corrugations or ribs of 3-9 mm at their depth of 0.3-2.0 mm with the shanks welded to them. The catalytic area is formed due to selection of the depth of the shanks greater, than the depth of the panels, owing to what at their assembly in compliance with shanks by means of welding between the panels are left the vertical slits of 5...20 mm width where fragments-granules of the catalytic agent are placed. The given engineering solution ensures conditions close to isothermal requirements of the synthesis through the whole volume of the reaction zone, ease of assembly and maintenance of the reactor in all climatic zones, and also in provision of its reliability, transportability and repairability.

EFFECT: the invention ensures conditions close to isothermal requirements of the synthesis through the whole volume of the reaction zone, ease of assembly and maintenance of the reactor in all climatic zones, its reliability, transportability and repairability.

3 cl, 6 dwg

FIELD: nuclear power engineering, transport, chemical mechanical engineering, and other industries.

SUBSTANCE: proposed method for recombining hydrogen and oxygen in gas medium meant to ensure hydrogen safety includes bringing of gas mixture in contact with heated catalyst body disposed along heat-conducting channel to ensure heat transfer between them. Temperature of heat-conducting channel hot end at point of its contact with catalyst body is maintained between 150 and 350 °C and temperature of its cold end at point of its contact with catalyst body is maintained below that of hot end. Gas mixture is passed through catalyst body from cold end of heat-conducting channel to its hot end. Hydrogen-and-oxygen recombiner has case with inlet and outlet sections, as well as heat-conducting channel disposed in-between and catalyst body placed on the path of gas mixture flow along heat-conducting channel. The latter is equipped on conducting end with cooling device and on outlet end, with heater. Hydrogen concentration working range is extended to 0.5 - 25% of gas mixture.

EFFECT: enlarged hydrogen concentration range, enhanced operating reliability under different operating conditions.

5 cl, 2 dwg

FIELD: chemical industry; a method of modernization of a completely detectable reactor.

SUBSTANCE: the invention is pertaining to the method of modernization of a completely detectable reactor. The method provides for modernization of an in-situ reactor of a heterogeneous exothermic synthesis having an external body with several located in it one over another and at some space from each other layers of a catalyst, at realization of which on the initial stage in the upper part of the body form at least the first layer of the catalyst filled in with the first catalyst having the activity picked beforehand; also form several layers of the catalyst located in the lower part of the body in parallel to each other. The layers located in the lower part of the body are filled in with the second catalyst, activity of which exceeds the activity of the first catalyst with which at least the first layer is filled in. The method of an exothermic heterogeneous synthesis with high yield is realized by feeding of the gaseous reagents in the reactor of a synthesis, which has a body with several catalyst layers resting on it, which are placed one over another at some space from each other and in which a reaction of interaction between the gaseous reagents runs. A reaction mixture also is fed at least from the first layer of the catalyst located in the upper part of the body into several layers of the catalyst located in parallel to each other in the lower part of the body. Let the reaction mixture run through the catalyst layers located in the lower part of the body and filled in with the catalyst the reaction activity of which exceeds activity of the catalyst, with which at least the first layer of the catalyst is filled in and the products of the reaction of the synthesis are taken out from the reactor catalyst layers located in the lower part of the body. The technical result is an increased conversion yield and productivity of the reactor at low operational costs and a low power consumption.

EFFECT: the invention ensures increased conversion yield and productivity of the reactor at low operational costs and a lower power consumption.

9 cl, 2 dwg

FIELD: initiating ammonia conversion reaction.

SUBSTANCE: proposed method is performed on reticular platinoid catalyst by passing the ammonia-containing gas mixture and oxygen-containing gas through it; local sections of catalyst surfaces are periodically heated to reaction initiating temperature by means of linear electric heating elements located directly on catalyst surface. Equivalent diameters of local sections of catalyst surface are selected between 1-5 of magnitude of external equivalent diameter of separate electric heating element; linear electric heating elements are connected to electric power source at duty factor from 20 to 1 s. Used as material for reticular platinoid catalyst are the following alloys: Pt-81, Pd-15, Rh-3.5 and Ru-0.5 mass-%; Pt-92,5, Pd -4.0 and Rh -3.5 mass-%; Pt-95 and Rh-5 mass-%; Pt-92.5 and Rh-7.5 mass-%. Initiating the ammonia conversion reaction by this method is performed in reactors for production of nitric and hydrocyanic acids and hydroxylamine sulfate.

EFFECT: reduction of time required for reaction over entire surface of catalyst; reduction of explosion danger.

2 cl, 10 ex

Reactor // 2246345

FIELD: chemical industry, catalytic processes.

SUBSTANCE: the invention presents a reactor for catalytic processes and is dealt with the field of chemical industry and may be used for catalytic processes. The reactor contains: a body; units of input and output for a reaction mixture and products of reactions; units of loading and unloading of a catalyst; a catalyst layer with the groups of the parallel hollow gas-permeable chambers located on it in height in one or several horizontal planes and each of the chambers has a perforated gas-distributing pipe with impenetrable butt connected to the group collector and used for input of additional amount of the reaction mixture. Each of perforated gas-permeable chambers is supplied with the second gas-distributing pipe with impenetrable butt. At that the impenetrable butts of the pipes are located on the opposite sides. The given engineering solution provides uniformity and entirety of agitation of the reaction mixtures.

EFFECT: the invention provides uniformity and entirety of agitation of the reaction mixtures.

5 cl, 4 dwg

The invention relates to a method for producing ammonia from a synthesis gas containing nitrogen and hydrogen, at a granular catalyst in at least one reactor under a pressure in the range from 50 to 300 bar and at a temperature in the range from 100 to 600°C; and from the reactor the mixture of products containing pairs of NH3divert, cooled, and the ammonia condenses and is separated with the formation of the recirculation gas, which is mixed with fresh synthesis gas and return the recirculated gas as synthesis gas in the reactor

Reactor // 2246345

FIELD: chemical industry, catalytic processes.

SUBSTANCE: the invention presents a reactor for catalytic processes and is dealt with the field of chemical industry and may be used for catalytic processes. The reactor contains: a body; units of input and output for a reaction mixture and products of reactions; units of loading and unloading of a catalyst; a catalyst layer with the groups of the parallel hollow gas-permeable chambers located on it in height in one or several horizontal planes and each of the chambers has a perforated gas-distributing pipe with impenetrable butt connected to the group collector and used for input of additional amount of the reaction mixture. Each of perforated gas-permeable chambers is supplied with the second gas-distributing pipe with impenetrable butt. At that the impenetrable butts of the pipes are located on the opposite sides. The given engineering solution provides uniformity and entirety of agitation of the reaction mixtures.

EFFECT: the invention provides uniformity and entirety of agitation of the reaction mixtures.

5 cl, 4 dwg

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