RU1781283C - Method for production of distillate - Google Patents

Abstract

SUMMARY OF THE INVENTION: A mixture of 60-60% tar and atactic polypropylene 10-40% is subjected to delayed coking. 2 tab.

Description

The invention relates to the field of thermodestructive processing of heavy oil residues and can be used in the refining industry in delayed coking plants.

It is known to use heavy oil residues as a raw material for coking resulting from oil distillation, deasphalting, thermal and catalytic cracking of residual and distillate fractions, gasoline pyrolysis and gas oil fractions.

The use of the aforementioned petroleum products as a raw material for coking involves the use of valuable commercial petroleum products and does not provide a high yield of coking products, especially distillate.

The closest to the claimed technical solution is the work where, as a raw material for delayed coking, a mixture of tar of Mangyshlak oil from a thermal cracking unit with the addition of a cracking residue of Martysh oil is used.

The disadvantage of this method is the use of Martyn oil as a cracking residue and a low yield of distillate (72.1-74.5 wt.%).

The aim of the invention is to increase the yield and improve the quality of the distillate.

This goal is achieved by adding to the tar of the Mangyshlak oil a fraction of atactic polypropylene (APP) in molten form (temperature 90-120 ° C) in a ratio of components, wt.%:

Tar 60-90

Atactic polypropylene 10-40 A mixture of tar of Mangyshlak oil with APP in certain proportions was coked at a flowing laboratory unit capable of reproducing the operating mode of factory settings. A reactor with a useful volume of 2 l, high. 300 mm Temperature 400-450 ° С. The heating of the apparatus for heating the feed mixture and the coking reactor is electric.

Tar of Mangyshlak oil from a thermal cracking unit has physic VI 00

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chemical indicators and composition shown in table 1.

The atactic fraction of polypropylene (APP) is a waste of the Guryev Chemical Plant named after 50th anniversary of Oct. Br; a non-standard product of iso-atactic polypropylene production is used, filtered from the solid phase (APP density 0.85 g / cm3, melting point 70-90 ° C). Conforms to TU 6-05-12-75.

Example 1. Tar of Mangyshlak oil in the amount of 270 g (90 wt.%) At a temperature of 90-120 ° C is mixed with 30 g (May 10.%) APP. The finished mixture at these temperatures is fed to a delayed coking reactor.

Process conditions: feed rate 0.13 hours; the temperature in the reactor is 400-450 ° C; pressure is atmospheric.

By coking, 227.4 g (75.8% by weight) of distillate are obtained, i.e., the yield of the latter, compared to known (2) (74.5% by weight), is increased by 1.7% by weight of the distillate.

Example 2, Under the conditions of Example I, from 240 g (80 wt.%) Tar and 60 g (20 wt.%) APP, 231.0 g (May 77.0%) of distillate are obtained, i.e. the yield of the latter is increased by 4.5% by weight of the distillate in comparison with the known (73.7 May,%).

Example 3. Under the conditions of Example 1, from 210 g (70 wt.%) Tar and 90 g (30 wt.%) APP, 234.0 g (78.0 wt.%) Of distillate are obtained, i.e. the yield of the latter compared with the known (73.3 May.%) increases by 6.4% by weight of distillate,

Example 4. Under the conditions of Example 1, from 180 g (60 wt.%) Tar and 120 g (40 wt.%) APP, 237.0 g (79 wt.%) Of distillate are obtained, i.e. the yield of the latter is increased by 7.9% by weight of the distillate compared with the known (73.2 wt.%).

Example 5. Under the conditions of example 1, from 150 g (50 wt.%) Tar and 150 g (50 wt.%) APP receive 243.0 g (81.0 may.%) Of distillate, i.e. the yield of the latter compared with the known (73.2 wt.%) increases by 10.6% by weight of the distillate.

Example 6. Under the conditions of Example 1, from 120 g (40 wt.%) Tar and 180 g (60 wt.%) APP, 249.0 g (83.0 wt.%) Of distillate are obtained, i.e. the yield of the latter is increased by 13.5% by weight of the distillate compared with the known (73.1 wt.%).

Example 7. Under the conditions of Example 1, from 90 g (30 wt.%) Tar and 210 g (70 wt.%) APP, 255.3 g (85.1 wt.%) Distillate are obtained, i.e. output of the latter compared to

known (72.9% by weight) increases by 16.6% by weight of distillate.

Example 8, Under the conditions of example 1, from 60 g (20 wt.%) Tar and 240 g (80 wt.%)

APP get 261.6 g (87.2 wt.%) Of distillate, i.e. the yield of the latter is increased by 20.1% by weight of the distillate compared with the known (72.6 wt.%).

Example 9. Under the conditions of example 1, from

0 30 g (10 wt.%) Tar and 270 g (90 wt.%) APP get 262.2 (87.4 wt.%) Distillate, i.e. the yield of the latter is increased by 21.2% by weight of the distillate in comparison with the known (72.1 wt.%).

5 The material balance of the coking process according to the proposed and known methods are given in table.2.

As can be seen from the table. 2, the addition of atactic polypropylene to the tar in an amount of 10 wt% and higher leads to an increase in the yield of distillate in comparison with the known method. However, with an increase in the amount of APP in the composition of the feed due to an increase in the yield of distillate, it decreases

5 yield of coke - one of the target products of the coking process.

So, if at a content of 40 wt.% In the feed, the coke yield is 15.6 wt.% Of the feed, then at a feed of 50

0 wt.% APP; coke yield decreases to 14.0 wt.%. It is known that a satisfactory coke yield that meets the design requirement of the ultrasonic testing complex of the Guryev Oil Refinery named after V.M. Lenin, equal to 15.0 wt.%. It means that

5, the amount of APP in the composition of the proposed raw material cannot exceed 40 wt.%, Otherwise the coke yield does not meet the design requirement of the ultrasonic inspection. Therefore, the optimal content of the APP in the composition of the proposed

0 feed is in the range of 10 to 40% by weight.

From the table. 2 it is also seen that in the proposed examples, the yield of the gasoline fraction of the distillate sharply increases - by 1.8-2.2

5 times, compared with the known. Therefore, the proposed method improves the quality of the distillate.

Thus, the proposed method for producing distillate by delayed

The tar coking using atactic polypropylene as an additive has the following advantages over the known one.

Distillate yield increases markedly

5 and its quality is improved;

The problem of recycling chemical industry wastes;

The use of chemical industry waste - atactic polypropylene - as one of the main

Claims (1)

components, the delayed coking feedstock saves the bulk of the basic feedstock, oil tar. SUMMARY OF THE INVENTION A method for producing distillate by delayed coking of tar, characterized in that, in order to increase yield and improve the quality of the distillate, atactic polypropylene is added to the tar and the following ratio of components is maintained, wt.%: Tar 60-90 Atactic Polypropylene 10-40 UTable Physico-chemical characteristics and hydrocarbon composition of the tar of Mangyshlak oil Table 1 The material balance of the coking of a mixture of tar of mangyshlakaya oil with atactic polypropylene (APP) at various contents compared to the known (2)