SU506302A3 - The method of producing liquefied petroleum gas - Google Patents

Description

City metals of Group VIII are contained in an amount of 0.01-2 isec. %

The hydrocracking process is carried out at 343-510 ° C. The most optimal temperature is 351-483 ° C. The pressure in the hydrocracking reaction zone is 70.3-175.8 kg / ss, the rate of hydrocarbon delivery is 0.25-5 units volumetric hourly velocity of the fluid. Hydrogen concentration m / bbl. As a hydrocracking catalyst, one OR several metals of the IVB and VII groups of the Periodic Table of the elements are used, for example, tin, germanium, nonscore on silica, containing 12-30 wt. % alumina.

In the second hydrocrack stage, a catalyst may be used in which the metallic components pore crystalline aluminosilicate molecular sieves. Mordenite, molecular sieves of types X and Y, as well as zeolite-containing material dispersed in an amorphous alumina matrix, silica gel or aluminosilicate can be used as molecular sieves.

Hydrocracking reactions I | are mainly exothermic reactions. With the passage of raw materials and hydrogen through the bed of the catalyst, an increase in temperature is observed. Therefore, in order to avoid a very high temperature increase in the hydrocracking zones IB, one or several points of these zones 1 supply cooling IHOTOK liquids or gases.

Example I. Production of liquefied petroleum gas from heavy hydrocarbon feedstock with a boiling point of 547 ° C.

In the drawing. Depicts the setup diagram for the implementation of this process.

Characteristics of raw materials:

Density,, 8756 Distillation interval, ° С: Starting point: boiling point 210 1.0% 338 30% 360 50% 377 70% 398 90% 448 Endpoint, 549 Sulfur, wt. % 0.93 Nitrogen, hours per million 600

 the raw material is hydrotreated using a catalyst consisting of a glyozem-cremiesel carrier containing 37 weight. % silica, 1.8 oats. % liquor, 16 wt. % molybdenum. The iB reaction zone maintains a pressure of 140 kg1 cm and a temperature in the catalyst bed of 455 ° C. The feed rate and raw material are 4500 bbl, the concentration of hydrogen is about 186 m / bbl, the volumetric rate of the liquid is 0.70. The hydrogen consumption in the hydrotreating system is 1.32% of the total weight of the fuel. Data on the yield and distribution of products during hydrotreatment are given in table. one.

t a b l ii c a 1

Output

Component

, l I bar.1} / day

From tab. 1 it follows that although the main

The reactions are desulfurization and denitration, a significant part (Products are cracked into low-boiling hydrocarbons. In a liquefied (Oil-gas, 111 barrels / day of propane-butane concentrate should be introduced;

The C7-200 ° C fraction in the amount of 634 bbl / day should be put on the second stage of hydrocracking.

4.03.5 bbl / day of hydrocarbons boiling above 200 ° C is used as feedstock for the two-stage 1 process fed through line 1. The ratio of hydrocarbons boiling above 200 ° C to the recycled liquid phase of the first stage of the process is 1, 6 The above raw materials in line 1 are mixed with

2,400 bbl / day of recirculated liquid phase of the first stage supplied by line 2 and i283 m / bbl of recycled hydrogen coming ino line 3.

The resulting mixture is directed along line 1

to the hydrocracking reactor 4, where the pressure is maintained at about 141 kg / cm and the temperature in the catalyst bed is about 400 ° C. The clock volume per fluid rate is 4,035 bbl / day of fresh raw material

0.81. The effluent falls along line 5 to the hot Cgparator 6 at a pressure of 146 kg / cm and a temperature of 204 ° C. In ta | bl. 2 shows the D output data and the composition of the Products coming from the reactor 4.

table 2

Output

The main ar-like phase, coming from the hot separator 6 through line 7, is connected to naphtha with naphtha in