SU1279997A1 - Method of producing petroleum coke - Google Patents

Abstract

The present invention relates to a method for producing petroleum coke on delayed coking plants, which allows an increase in the yield of petroleum coke. The hydrocarbon feedstock enters the tube furnace 1, from where heated to 380-400 ° C enters the distillation column 2, where it is fractionated into light fractions and cubic residue. The latter is heated in the furnace 1 to 475-510 0 and fed to the separator 3 for separating the vapor-gas products. The liquid part of the bottom residue is directed to the bottom of the reactor 4 for coking. The separated vapor-gas products are fed to the top (L of the reactor 4 above the level of its filling with coke. 1 ill., 1 tab. /

Description

The invention relates to the oil refining and petrochemical industries, in particular, to a method for producing petroleum coke in delayed coking plants.

The purpose of the invention is to increase the yield of coke.

The drawing shows a process flow diagram of a method for producing petroleum coke.

The tube furnace 1 is connected to the distillation column 2 and to the separator 3, which is connected to the coking reactor 4 and to the distillation column 2.

The proposed method is carried out as follows.

The feedstock, such as tar from West Siberian oil, enters the tube furnace 1, from where it reaches 380–400 ° C and enters the distillation column 2, where it is fractionated into light fractions and bottoms. The latter is heated in a furnace 1 to 475-510 ° C is fed to a separator 3, where steam-gas products are separated from the bottom residue. The liquid part of the bottoms residue is directed to the lower part of the reactor 4 for coking, the separated vapor-gas products are fed tangentially to the upper part of the reactor 4 above the level of its filling with coke. At the same time, due to the additional separatism of the vapor-gas products separated in the separator 3, part of the coke-forming components remains in the reactor 4 and coke 5 forms additional coke. The decomposition and additional separation products (gases, gasoline, gas oils) from the top of the reactor 4 enter the distillation column 2 in contact with the feedstock.

Example 1 Under laboratory conditions, the feedstock (tar from West Siberian oil), heated to 400 ° C in a kiln, is strained into a distillation column, where it is fractionated into light fractions and bottoms. The bottoms are heated from the furnace to 480 ° C and sent to a separator, where it is separated into vapor-gas and liquid parts. The liquid part is directed to coking in the lower part of the reactor at 480 ° C and a pressure of 0.1 MPa for 5 hours, and the separated vapor-gas phase (,

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300 ° C), the composition of which is given in the table, in the upper part of the reactor above the level of filling the reactor with coke. With this steam vapor products sent to the reactor are involved in the coking process and give an additional amount of coke.

The total coke yield is 20.1%.

Example 2. B of the conditions of example 1, i.e. All stages of the process before the separation of the bottoms residue heated to 480 ° C are similar; the separated vapor-gas part (T ZOO ° C), the composition of which is shown in the table, is directed downward in the rectification column, and the liquid part is coked in the reactor at 480 ° C and at a pressure of 0.1 MPa for 5 hours.

The coke yield (from the liquid part of the bottom residue) is 18.9%.

Example Under the conditions of Example 1, vapor-gas products whose composition is similar to that given in the table are separated in a separator, and the liquid phase (heavy part) is coked in a reactor at 440 ° C and a pressure of 0.1 MPa for 5 hours. of the heavy part of the raw material is 18.9%.

Comparison of examples 1 and 2 shows that when coking using the proposed method, the yield increases. coke (by 1.2%), coking ability of steam-gas products entering the distillation column (2.5 times), and the content of coke-forming components (by 7.5%) decrease.

Thus, the proposed method will allow increasing the coke yield due to the involvement of an additional amount of coke-forming components from the steam-gas products in the reactor. The content of coke-forming components in vapor-gas products entering the distillation column is reduced accordingly.

In addition, the supply of vapor-gas products to the upper part of the chamber will reduce the height of the foam in the reactor.

Claims (1)

1. Composition, wt.% Paraffin-naphthenic hydrocarbons Aromatic hydrocarbons: After separationAfter torus reactor 41.9 46.0 74 of the reactor, characterized in that, in order to increase the output of coke, the separated vapor-gas products are fed for coking into the upper part of the reactor above the level of its filling with coke.