Reactor for the catalytic dehydrogenation of hydrocarbons

 

(57) Abstract:

The invention relates to a device for the catalytic dehydrogenation of hydrocarbons, in particular for radial flow reactors, and can be used in the chemical and petrochemical industries. The objective of the invention is the efficiency of the reactor due to the uniform distribution of flow of the reaction mixture. Proposed reactor for the catalytic dehydrogenation of hydrocarbons containing cylindrical body coaxially mounted an annular basket with a catalyst made of inner and outer perforated cylinders, and fairing in the form of a conical body of revolution, located in the inner perforated cylinder. Used the body of rotation is at an altitude of three parts: the base - cylindrical, the height of which is 0,02-0,25 L, when the top - hemispherical, the height of which is 0,005-0,05 L, and the medium for which: where Rtis the radius of the current section of the middle part of the body of rotation; RNR- the radius of the inner perforated cylinder; h is the distance from the top of the body of revolution to its current cross section; L is the height of the body of rotation. The cross-sectional area of the basket with cateechee-sectional space between the casing and the outer perforated cylinder is 1-5 squares of the cross-section of the inner perforated cylinder. The area of the free cross section of the perforations of the inner cylinder is 1-20 of squares of its cross section. The area of the free cross section of the perforation of the outer cylinder is 0.5-6 square free cross section of the perforations of the inner cylinder. The use of this reactor allows to increase the efficiency of the catalytic dehydrogenation and improve the quality of the final product. 4 C.p. f-crystals, 1 Il.

The invention relates to a device for the catalytic dehydrogenation of hydrocarbons, in particular for radial flow reactors, and can be used in the chemical and petrochemical industry for the dehydrogenation of ethylbenzene to styrene, isoamylenes in isoprene, butylene to butadiene, etc.

Known reactor axial type to obtain styrene, consisting of a cylindrical body, filled with a layer of immobile coarse catalyst. (N.N. Lebedev "Chemistry and technology of basic organic and petrochemical synthesis. Chemistry, 1975, page 575). Known reactor has a large height of the catalyst layer and, accordingly, a large pressure difference across the layer (hydraulic resistance), which leads to low dehydrogenation. In addition, the Sz because of their relatively low productivity.

Closest to the proposed reactor and devoid of these shortcomings is the radial reactor type for the catalytic dehydrogenation of hydrocarbons containing cylindrical body coaxially mounted an annular basket with a catalyst made of inner and outer perforated cylinder, inside which are placed coaxially fairing in the form of a body of rotation (EN 2154523 Cl, 20.08.2000 year). However, the disadvantage of this reactor is concluded that its design does not provide a uniform distribution of flow of the reaction mixture throughout the volume of the catalyst, which reduces the efficiency of the process and affects the quality of final products.

The objective of the invention is the efficiency of the reactor due to the uniform distribution of flow of the reaction mixture.

Proposed reactor for the catalytic dehydrogenation of hydrocarbons containing cylindrical body coaxially mounted an annular basket with a catalyst made of inner and outer perforated cylinders and fairing in the form of a conical body of revolution, located in the inner perforated cylinder. Used body rotation is the height of the TA which is 0,005-0,05 L, and average, which is:

< / BR>
where Rtis the radius of the current section of the middle part of the body of rotation;

RNR- the radius of the inner perforated cylinder;

h is the distance from the top of the body of revolution to its current section;

L - height of the body of rotation.

In the proposed reactor:

- the cross-sectional area of the basket with the catalyst is 0.5 to 6 squares of the cross-section of the inner perforated cylinder;

- the cross-sectional area of the space between the casing and the outer perforated cylinder is 1-5 squares of the cross-section of the inner perforated cylinder;

- the area of the free cross section of the perforations of the inner cylinder is 1-20 of squares of its cross section;

- the area of the free cross section of the perforation of the outer cylinder is 0.5-6 square free cross section of the perforations of the inner cylinder.

The drawing shows a diagram of the proposed reactor for the catalytic dehydrogenation of hydrocarbons. The reactor comprises a cylindrical housing 1 in which is coaxial outer 2 and inner 3 perforated cylinders that make up the basket, which concluded layer katalysator cylindrical part "a", hemisphere, and between them the middle part "C" with the changing height of the geometry of the outer surface. The middle part "C" can be performed, for example, in the form of a set of truncated cones (see drawing).

The reaction mixture through the nozzle 6 is fed into the internal cylinder 3, which surrounds the fairing 5, passes sequentially through the holes of the perforated cylinder 3, the catalyst layer 4, the holes of the perforated cylinder 2 and through the nozzle 7 leaves the reactor.

The proposed form of the fairing provides a reactor for the catalytic dehydrogenation of hydrocarbons uniform distribution of flow of the reaction mixture throughout the volume of the catalyst loaded in an annular basket.

The use of the proposed reactor for the catalytic dehydrogenation improves the efficiency of the catalytic dehydrogenation of ethylbenzene to styrene and to improve the quality of the final product.

1. Reactor for the catalytic dehydrogenation of hydrocarbons containing cylindrical body coaxially mounted an annular basket with a catalyst made of inner and outer perforated cylinders, and fairing in the form of consobrina body rotation, the Oita height of three parts: the base - cylindrical, the height of which is 0,02-0,25 L, when the top - hemispherical, the height of which is 0,005-0,05 L, and the medium for which

< / BR>
where Rtis the radius of the current section of the middle part of the body of rotation;

RNR- the radius of the inner perforated cylinder;

h is the distance from the top of the body of revolution to its current section;

L - height of the body of rotation.

2. The reactor under item 1, characterized in that the cross-sectional area of the basket with the catalyst is 0.5 to 6 squares of the cross-section of the inner perforated cylinder.

3. Reactor PP.1 and 2, characterized in that the cross-sectional area of the space between the casing and the outer perforated cylinder is 1-5 squares of the cross-section of the inner perforated cylinder.

4. Reactor PP.1 to 3, characterized in that the free cross section area of the perforations of the inner cylinder is 1-20 of squares of its cross section.

5. Reactor PP.1 to 4, characterized in that the free cross section area of the perforations of the outer cylinder is 0.5-6 square free cross section of the perforations of the inner cylinder.

 

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FIELD: sorption neutralization of gases.

SUBSTANCE: proposed device includes two parallel horizontal gas-tight reactors arranged in casing at spaced relation; each reactor includes at least two sections filled with bulk granulated adsorbent and closed over ends with partitions carrying ejection pneumatic haulage units mounted above flow divider; device is provided with inlet and outlet branch pipes for delivery and discharge of gas; provision is made for V-shaped slide at angle of generatrices exceeding slope of repose for bulk adsorbent; V-shaped slide of each reactor is provided with drain branch pipe; walls of central reservoir are combined with hood excluding bridging of adsorbent; hood is equidistant relative to slide. Mechanism for hermetic discharge of used adsorbent includes longitudinal screw feeder and discharge pipe fitted with swivel gate valve; direction of turn of spiral provided on screw feeder of discharge mechanism is opposite to direction of main spiral.

EFFECT: improved quality of neutralization of gases; enhanced operational safety.

2 cl, 6 dwg

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