SU1710118A1 - Catalytic reactor - Google Patents

Abstract

The invention relates to oil refining and petrochemistry, in particular to reactors for carrying out catalytic processes such as catalytic reforming, paraffin dehydrogenation, and improves the efficiency of the reactor operation due to uniform distribution of the gas raw material mixture in the catalyst bed. The catalytic reactor contains a vertical case with bottoms, fittings for introducing gas-raw mixture and withdrawal of reaction products, loading and unloading pipes, an annular catalyst chamber with solid and perforated walls formed by external and internal conical and cylindrical shell. New in the reactor is the installation of a solid cylindrical partition located coaxially with the casing and connected to the upper end of the outer cylindrical shell. 1 Cp. Of the field, 4 sludge. The invention relates to the field of oil refining and petrochemistry, in particular, to the design of reactors for carrying out catalytic processes, such as catalytic reforming, paraffin dehydrogenation, etc. A reactor with a stationary layer is known. catalyst for carrying out catalytic processes, containing a vertical case with bottoms, fittings for introducing a gas-raw mixture (GSS) and withdrawal of reaction products (PR), an annular catalyst chamber with continuous and perforated walls formed by external and internal The other conical and cylindrical shells. The disadvantages of this reactor design are the uneven distribution of GSS in the catalyst bed, as well as the possibility of operating in a moving catalyst bed. The known design of a catalytic reactor with a moving catalyst bed (Fig. 1), which contains a vertical casing with bottoms, fittings GSS input and output PR, loading and unloading pipes, annular catalyst chamber with solid and perforated walls formed by the outer and inner co matic and cylindrical obechaykami.Odnako known structure does not provide uniform distribution in the catalyst bed REG. This is due to the fact that the GSS jet, traversing face A (Fig. 2), due to the inertial forces of gas particles coming from section T to section 2, is compressed and then expanded. As a result of the inertial detachment of the GSS jet from the perforated sheet, ^ O 00! ≫ &

Description

The seagulls 3 form a circulation area B, filled with a multitude of vortices. This area is characterized by a reduced gas pressure, which causes leakage into it through the perforation holes of the channels from the catalyst bed of the reaction mixture. As a result, in part of the catalyst bed B (Fig. 2), ordered and uniform filtering of the GSS is disturbed. This results in a decrease in this part of the total volume of the catalyst bed, in which uniform filtration of the reaction mixture in the radial direction remains unchanged. As a result, the useful volume of the catalyst bed is reduced, which is confirmed by the results of an examination of the operation of industrial reactors, and this reduces their efficiency.

The aim of the invention is to increase the efficiency of the reactor operation by uniformly distributing the gas-source mixture in the catalyst bed.

The catalytic reactor containing a vertical case with bottoms, fittings for input of the GSS and output PR, loading and unloading pipes, rings of the catalyst chamber with solid and perforated walls formed by the outer and inner cylindrical and conical shell, is equipped with a solid cylindrical partition, coaxial with the case and connected to the upper end of the outer cylindrical shell. In this case, the height A of the solid cylindrical partition is (1.5-4). (D - d), where D and d are the diameters of the vertical casing and the solid cylindrical partition, respectively.

Analysis shows that the proposed solution provides an opportunity to improve the efficiency of the reactor operation.

On fig.Z presents the reactor, the general view, and the scheme of its work; figure 4 - node I fig.Z.

The catalytic reactor consists of a cylindrical body 1, the upper 2 and the lower 3 bottoms, the fitting 4 of the GSS input and the fitting 5 of the output PR, the loading 6 and the discharge 7 pipes, an annular catalyst chamber 8 with solid and perforated walls formed by the shells: conical - outer 9 and internal 10, cylindrical - external 11 and internal 12, continuous cylindrical partition 13.

The reactor is intended to operate in three modes: with a stationary layer of catalyst (there is no movement / catalyst in the catalyst chamber), with a moving layer (in this case,

constant replacement of coked catalyst withdrawn from the lower part of the reactor with fresh one entering the reactor from above), semi-continuous mode of operation (combination of the first and second modes of operation, in this case replacement of the spent catalyst with fresh one begins when it reaches the specified content: coke).

0 The reactor operates as follows.

I

GSS enters the reactor through nozzle 4. Then through the perforated walls of the outer conical 9 and cylindrical 11

5 shells, the gas flow in the radial direction enters the catalyst chamber 8, from where the PR through the perforated perforated shell 12 and then the fitting 5 is led out of the reactor. The formation of the circulatory zone of the vacuum area B due to the inertial separation of the jet, starting from the top edge (point A, figure 4) of the cylindrical partition 13, occurs only in the annular channel between

5 by this partition 13 and the housing 1. This eliminates the intake of region B of the reaction mixture from the catalyst bed, which makes it possible to maintain a uniform and ordered filtering of GSS in the entire volume of the catalyst and accordingly increase its useful volume. The fresh catalyst is introduced into the catalyst chamber in order to replace the spent catalyst with it, followed by the latter being sent for regeneration using loading pipes 6. The spent catalyst is removed from the catalyst chamber through discharge pipes 7. Starting from loading pipes 6 into the annular

0, the catalyst chamber 8 and ending with the discharge pipes 7, the downward movement of the catalyst occurs under the action of gravity in the dense bed mode. The height D of the partition 13 is (1.5-4). (D

5 - d), i.e. 1,5 - 4 - hydraulic diameters of the annular channel formed between the vertical case 1 and the continuous vertical partition 13, selected on the basis of the general laws of gas flow

0 and liquids through nozzles, taking into account the need for minimum hydraulic resistance of the annular channel.

The use of the proposed design in comparison with the known allows

5 to increase the efficiency of the reactor operation by uniformly distributing the gas-raw mixture in the catalyst bed.

Claims (2)

1. A catalytic reactor containing a vertical case with bottoms, a fitting for introducing gas-raw mixture and withdrawal of reaction products, loading and unloading pipes, an annular catalyst chamber with solid and perforated walls formed by outer and inner conical cylindrical shells, characterized in that the efficiency of the reactor operation due to the uniform distribution of the gas and oil mixture throughout the entire volume of the catalyst chamber; the Gz2o reactor: Die Ea (. free) cooling tank (Cf). (tro otnon1 sh. xgta / and ator (OK flpodl / hty DSQifLfuu 9uf. / Phage. 2 is provided with a cylindrical partition located coaxially with the housing and connected to the upper end of the outer cylindrical shell. 2. The reactor according to claim 1, wherein the height of the solid cylindrical partition is (1.5-4). (D - d), where D and d are the diameters of the vertical shell and solid cylindrical partitions, respectively.