SU1715823A1 - Method of processing vacuum gas oil - Google Patents

Abstract

The invention relates to refining, in particular the processing of vacuum gas oil. The goal is to increase the yields of butane-butyl ene fraction and high-octane gasoline. For this, the bottom of an elevator reactor for contacting at 620-740 ° C (contact time 0.5-2.5 s) with a regenerated cracking catalyst in the presence of 5-10 wt.% Octane elevation additives containing a high-silica zeolite of the type ZSM- 5, 5-10% (by weight of the initial vacuum gas oil) gasoline fraction of thermal origin is fed at the mass ratio of the catalyst with the additive and the gasoline fraction (60-, 120): 1. The original vacuum gas oil is fed to a point above the feed point of the gasoline fraction. Such conditions allow an increase in the yield of the butanbutylene fraction by 3.5 wt.% And high-octane gasoline per / v 1 wt.%. 3 tab. 3 (L

Description

The invention relates to a method of The treatment of vacuum gas oil by catalytic cracking in an elevator reactor with the production of gasoline, propane propylene and but tanutylene fraction as target products can be applied in the refining industry.

A known method of catalytic cracking with the production of middle distillates is that neper, the gas oil is processed in the presence of added olefin-containing naphtha (olefin content in naphtha. 10% by volume). The volume ratio of naphtha to gas oil is (20-40);

: (80-60). There is an increased yield of middle distillates.

The disadvantage of this method is (the fact that the addition of a significant amount of olefin-containing naphtha to the main feedstock leads to a decrease in the octane number of the gasoline fraction obtained.

The known method of catalytic cracking, according to which in order to maintain a predetermined temperature range of the catalyst flows, a diluent — naphtha (hydrocarbons like gasoline) is added to the latter, the partial pressure of the feed is controlled by maintaining a certain ratio

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 J: 17

the diluent and the feed, the diluent is injected at a point with a temperature higher than at the feed point, as a result, a significant portion of the naphtha and the feed is cracked.

The disadvantage of this method is that when naphtha is supplied to a point with a high temperature and cracked, a significant part of it increases the yield of dry gas and decreases the selectivity of the process.

The known method of catalytic cracking using naphtha. Safety is used to produce high-octane gasoline and other valuable products from stripped petroleum, oil residues. The method is as follows: in / line of the main hydrocarbon feedstock,

However, a long contact time in the catalyst mixing zone with the benzene fraction of the paraffin base requires special devices. In addition, the method peculiar to.

25

yafta boiling between 71-204 ° C, 20 output of the butan-butylene fraction and then the mixture is fed to contact with a hot catalyst to the bottom of the riser reactor. Ratio catalyst total feedstock is (2-12): 1 naphtha and catalyst are moving: vv px for the lift reactor. The residence time of naphtha in the riser reactor is 0.5-10 s, temperature 482-7600С, pressure-. denie 0, 4 ata. The amount of naphtha added is 1-10% by weight of sulfur. Naphtha contains at least 10% of naphthenic hydrocarbons, mainly c. as cycdopentane and cyclohexane. . Naphtha is used as a hydrogen donor. The latter has a greater n / s ratio than the main raw material. AT

Sokooctane gasoline.

The purpose of the invention is to increase the output of the butanbutylene fraction and high-octane gasoline. The goal is achieved in that according to the method of processing vacuum gas oil by cataditating cracking using an elevator reactor when the last gasoline fraction is fed to the bottom of the gas line to contact with regenerated catalytic cracking catalyst in the presence of an octano-enhancing additive .- a high-silica zeolite of the type ZSM-5, taken in an amount of 5-10 wt.%, calculated on the catalyst, used zuyut gasoline fraction thermal origin,

thirty

As a result, propane, butane, butylene, and benzene fractions are obtained.

40

Zine, boiling away within the NK 221 C.

A significant residence time in the naphtha lift reactor and a high temperature in the reaction zone cause deep naphtha cracking, which leads to a significant yield of dry gas and, as a consequence, a decrease in the yield of the target gasoline and valuable butanbutylene fraction. In addition, naphtha is added to the feedstock, having a low octane content. the number 45 p AI (research method) reduces the octane characteristics of the gasoline being produced. - The closest to the proposed. is a method of processing vacuum S5

The gasoline fraction of thermal origin (thermobenzene) is fed to the bottom of the riser reactor for contact with the regenerated catalyst containing octane-based additive in

foot gas oil by catalytic

cracking using a lift-reaction-based zeolite of the ZSM-5 type, for example, a torus. At the bottom of the latter, a benzene ultrahigh-silica (VCS) zeolite fraction of the paraffin base is fed, the content of the catalyst is the ratio of (French or C-j-Cy) t It is subjected to the ny AlgOeb35, and the main raw material

contact with a cracking catalyst containing an octane additive ZSM-5. Vacuum source gas

like

Soil served at a point above the point of supply of the gasoline fraction. The ratio of catalyst to raw materials is from 50: 1 to 200: 1 (with precontacting), temperature 593-815 ° C, contact time from 10 to 50 s. The process uses a catalytic cracking catalyst containing an octane-boosting additive - a zeolite of the type ZSM-5 (high-silica zeolite).

However, a long contact time in the catalyst mixing zone with the gasoline fraction of the paraffin base requires special devices. In addition, the method peculiar to.

the output of the butane-butylene fraction and you

Sokooctane gasoline.

The purpose of the invention is to increase the output. yes butanutylene fraction and high; octane gasoline. The goal is achieved in that according to the method of processing vacuum gas oil by cataditic cracking using an elevator reactor when the last gasoline fraction is fed to the bottom of thermal origin for contact with the regenerated catalyst of catalytic cracking in the presence of an octane upgrading additive. a high-silica zeolite of the ZSM-5 type, taken in an amount of 5-10% by weight, based on the catalyst, uses a gasoline fraction of thermal origin,

the contacting is carried out at 620 -, the contact time is 0.5-1.5 s, the amount of the gasoline fraction is 5-10% by weight of the initial vacuum gas oil, the mass ratio of the catalyst with the additive to the gasoline fraction (60-120): 1 and the supply of vacuum gas oil to a point above the feed point of the gasoline fraction.

The essence of the proposed method is as follows.

The gasoline fraction of thermal origin (thermobenzene) is fed to the bottom of the riser reactor for contact with the regenerated catalyst containing octane-based additive in

The basis of a zeolite of the ZSM-5 type, for example, a ultra-high-silica (SEC) zeolite-containing catalyst, the ratio A1gOeb35, and the main raw material

17

vacuum gas oil, served at a point above the zone of contact of gasoline and catalyst.

The amount of gasoline introduced is 5-10% by mass on raw materials. The amount of octane-supplement added is 5-10% by weight per catalyst. The ratio of the catalyst with the octane additive and thermobenzene is (60-120): 1.

A large ratio of additives to thermal benzine, high temperature in the contact zone (620–740 3С) contribute to the selective transformation of low cortical olefins contained in thermal

Zinah in an amount up to 40 May,%, in high-octane components and light olefins. Diluted with thermobenzene. the phase of the catalyst comes in contact 10 with the main raw material. The main raw material, vacuum gas oil, cools the mixture of catalyst, additives and products of high-temperature cracking of thermal benzine to a cracking temperature of 500-520 ° С.

The characteristics of the used catalysis cracking Da-250 and alkylation additive-g and Octup1

The amount of gasoline injected is 7 wt.% Per raw material, the amount of octane of the boosting additive of the composition by example is 17 wt.%. the catalyst, the mass ratio of the catalyst (with water) and thermobenzine is 100: 1, the temperature in the zone of contact between thermobenzene and talizator is 700 Cj and the contact time is 1

As a result of cracking, 50.1 wt.% Is obtained. target gasoline fraction with an octane rating of 91.6 p MI and 12.35 wt.% butanbutylene fraction

Example 4. The cracking was carried out according to example 1, while the number

(Japan) containing SVK-zeolite, about 30 benz ins 3 wt.%, Amount

Table of the characteristics of zeolite ZSM-5, are presented in Table. one.

Example. The low-octane gasoline fraction (thermobenzene) with a boiling point of 51-204 ° C, containing 3 38.3 wt.% Olefins, with an octane rating of MM (motor method), is introduced into the bottom of the lift reactor in an amount of: 5 wt.%, where they are in contact with the regenerated catalyst Yes-250 containing 5 wt.% of an octane-increasing additive (a VCS-zeolite-containing catalyst with a ratio of SiO iAljO SS), the temperature in the contact zone is 620 ° С, the mass ratio of the catalyst with octant with booster additive and thermrbenzene. 60: 1.

Osnrvnre raw materials - vacuum gas oil boiling at a temperature above

324 ° C, served above the point of entry thermo- 3 gasoline. Contact time 0.5 s. As a result of cracking, 49.9 wt.% Of the target gasoline fraction with ca. / gan number of 91.2 p. MI and 11.14 wt.% Are obtained. butanbutylene fraction.

Note 2. The cracking is carried out as in Example 1. The amount of the introduced thermal benzine is 10% by weight, the temperature is d

the zone of thermobenzene contact with a regenerated catalyst containing 10 wt.% octane-enhancing additive (UHV-zeolite-containing catalyst with a ratio of .35) is 740 ° С, the mass ratio of the catalyst with the additive and thermobenzene is 120: 1, the contact time is 1.5 s.

Get 49.7 wt.% Target gasoline fraction with an octane number of 91.7 p MI and. 12.72 wt.% Butanbutylene fraction.

Example 3. The cracking is carried out but Example 1 ,.

The amount of gasoline injected is 7 wt.% For raw materials, the amount of octano-enhancement additive of the composition according to example 17 wt.%. catalyst, mass ratio of catalyst (with additive) and thermobenzine 100: 1, temperature in the contact zone of thermobenzine and ka-t catalyst, 700 Cj contact time 1 s,

As a result of cracking, 50.1 wt.% Is obtained. the target gasoline fraction with an octane number of 91.6 p MI and 12.35 wt.% butanutylene fraction, 1

Example 4. Cracking is carried out as in Example 1, wherein the amount of

  benzoin 3 wt.%, amount

octano-rising additive 3 wt.% (as in example 1), the mass ratio of the catalyst (with the additive) is thermobenzene .40: 1, the temperature in the contact zone is 600 ° C, the contact time is 0.3 s.

Cracking results in 49.5 wt.% Of the target gasoline fraction with an octane rating of 89.9 p MI and 11.0 wt.% Of the butanbutylene fraction.

PRI me R 5. Cracking is carried out according to example 1, while the amount of gasoline introduced is 15% by weight for raw materials, the amount of octane-raising additive (as in example 1) is 15% by weight for catalyst, the mass ratio of catalyst (with additive) and thermobenzene 150: 1, temperature in the contact zone 76 € С „

The result is 48.6 wt.% Target gasoline fraction with an octane rating of 90.1 p MI and 10.77 wt.% Of the butanbutylene fraction.

The mode data of the process according to examples 1-5, as well as the data obtained therewith are given in table. 2

From the data table. 2 that at a process temperature below 620 C, pk-

The tane number of the target gasoline fraction is significantly reduced.

At temperatures above 740 ° C, the selectivity of the gasoline process decreases and the yield of dry gas significantly increases.

An increase in the mass ratio of the catalyst (with an octane additive) and thermobenzene contributes to an increase in the yield of coke and dry gas, to a decrease in the octane number and gasoline output. .

A decrease in the ratio of catalyst (with an octane additive) to thermal benzene causes a decrease in the yield of the propane propylene and butanbutylene fraction while reducing the octane number.

Increasing the amount of octane additive added is not economically justified.

Reducing the amount of additive does not allow to obtain the target gasoline fraction, with a given octane number.

In tab. Figure 3 shows the process data when using gasoline fractions of a paraffin base and thermal origin (thermobenzene) under the same operating conditions.

| Thus, the proposed method

j allows you to increase the yield of butanbutyl

new fraction from 9.13 to 12.64 wt.%

five

0

five

0

five

and about 1 wt.%. high octane gasoline output. In addition, by reducing the contact time of the gasoline fraction, the process technology is simplified.

Claims (1)

Invention Formula Vacuum gas oil processing method by catalytic cracking using a riser reactor when the last gasoline fraction is fed to the bottom for contacting the catalytic cracking catalyst regenerated in the presence of ZSM-5 zeolite octane additive and the original vacuum gas oil is above the feed point gasoline fraction, to obtain the desired products, which are used for the purpose of increasing the yield of the butanutylene fraction and high-octane gasoline, to use the gasoline fraction Thermal origin, contacting is carried out at 620-740 ° C, contact time 0.5-1.5 s, amount of octane-enhancing additive 5-10% by weight, calculated on catalyst, amount of gasoline fraction 5-10% by weight of the original vacuum gas oil and mass ratio of the catalyst with the additive - gasoline fraction (60-120): 1. Table 1 Indicator The temperature in the contact zone, ° C The quantitative ratio: of catalyst and thermo-gasoline of catalyst and total feedstock Amount of injected, wt.%: Naphtha gasoline The amount of octa-nano additive, wt.%. Contact time with: thermobenzene and catalyst. total feedstock and catalyst Material balance, wt.%: Dry gas. Supropane-propylene fraction 1715823 1 ° Continuation of table 1 table 2 The proposed method (for example) 740 700 600 760 120 100 40 150 ten 15 ten 15 1.5 1.0 0.3 2.0 2.0 5.94 1.73 1.44 3.91 . 00 5.8 5.92 C-Butanbu Gillen fraction gasoline: -five 221 ° C The temperature in the contact zone, C The quantitative ratio of the catalyst and gasoline fraction The amount of input gasoline, wt.% Amount of octopene addition, wt.% Thermal benzine and catalyst contact time, with Material balance, wt.%; dry gas C-propane pro-propylene fraction S-butanbutylene va fraction C25 gasoline 2050C Gasoline octane number, m MM IM Continued table. 2 12.72 12.35 11.00 10.77 T a b c a 3 665 665