SU1599359A1 - Method of producing benzene - Google Patents

Abstract

The invention relates to the production of hydrocarbons, in particular the production of benzene used in petrochemistry. The goal is to increase the yield of the target product. Synthesis of benzene is carried out by catalytic dehydrocyclization of hexene-1 in the presence of O ₂ -air at their volume ratio of 1: (3-6), contact time 0.06-0.9 s, bulk flow rate of the feed is 4000-6000 h ^-1 , preferably at 530 ° s One of the following contacts is used as a catalyst: a) CRO ₃ and MO ₂ O ₃

b) MO ₂ O ₃ and ZNO

c) CRO ₃ and HNO, atomic ratio of metals 1: (0.5-2), g) CRO ₃ + MOO ₃ + ZNO, atomic ratio 1: (0.5-2) :( 0.25-4), applied on AL ₂ O ₃ in the amount of 3-7 wt.%. These conditions provide an increase in benzene yield from 56.3 to 71% at a conversion of * 98–90% and a selectivity of 72%. 1 hp ff. 3 tab.

Description

The invention relates to methods for producing benzene, in particular to methods for producing benzene by dehydrocyclization of hexene-1 and can be used in the petrochemical industry.

The aim of the invention is to increase the output of benzene.

The method is illustrated by the following examples.

Example 1. 0.9 g Cr (N03) 3 x X and 0.21 g gp (CH 3 SOO) 2. dissolved in such amounts of 10% HNOj, so that the total volume of the solutions during draining does not exceed 6 ml. This solution is poured 10 cm (5.0 g) -y-Al Oj. After 1 h, the excess solution is drained. The catalyst is dried at 110-120 ° C for 2-2.5 hours and

calcined for 1 hour at and then 2 hours at.

The resulting catalyst contains 5 wt.% The active mass of the composition of ZnO.

The process is carried out in a laboratory setup in a fixed bed flow glass reactor.

catalyst. t

A prepared, 10 cm catalyst is loaded into a flow through glass reactor. The reactor is placed in a metal bash with a winding and fluidized sand, in which the desired temperature is maintained automatically.

The contact time varies by changing the volumetric feed rate.

SL

 with

00

ate with

31599359

Hexene - 1 mixed with air in a certain proportion through evaporation; the hoist enters the reactor. The volumetric rate is varied by varying the amounts of the fed components. Exhaust gas passes through a condensation system, liquid products are collected in a collection, and gaseous gases are vented.

3

about

m p

As can be seen from the table. 1-3, the proposed method allows increasing the yield of benzene from 1-hexene to 71% by weight against 56.3% by weight in a known way. In this case, the conversion of 1-hexene to 90%,

through the neutralizer to the atmosphere. The liquid benzene selectivity reaches

These products are rather easily separated by distillation, since the boiling point of hexene-1 is 63 ,, 1,5-hexadiene -, benzene -.

Hexadiene forms about 0.5% and can be distilled by an ace mixed with hexane, which can be recycled, since hexadiene is an intermediate between hexene and benzene.

Examples 2-15. The catalysts are prepared analogously to example 1.

Example 16. Oh, 33 g of chromium

- 72%. The process does not form any other aromatic hydrocarbons, which greatly facilitates the separation of benzene; the whole process is simplified by the process.

Claims (2)

1. A method of producing benzene by degating by cyclizing hexene-1 in the presence of a catalyst containing a metal oxide of group VI and γ-alumina, at a different temperature, o, l and h, and so that nitrate acid Cd (MO3) - 9H203 0.07 g 25 ° Increase the yield of benzene, ammonium ismine (MH) x to HjO and 0.30 g of zinc acetate (CZnCCH COO) dissolved separately in such amounts of 10% ; HNpg, so that when blending solutions ; their total volume did not exceed 6 w. i Pour 10 cm y-A1 O with this solution. : After 1 h, the excess solution is drained. ; Drying and calcining are similar to those described in Example 1. The resulting catalyst contains 5 wt.% Of the active mass. The composition — MoO — ZnO with a metal ratio of 1: 0.5: 2. In the presence of the obtained catalyst, the method is carried out analogously to example 1. The conditions and test results are shown in Tables 1-3. Examples 17-27. The catalysts are prepared analogously to example 1. use a catalyst containing oxides of chromium (III) and molybdenum (VI) or oxides of molybdenum (VI) and zinc, or oxides of chromium (III) and zinc with an atomic ratio of the specified metals 1: (0.5-2), respectively, or oxides chromium (III), molybdenum (VI) and zinc at an atomic ratio of 1: (0.5-2) :( O, 25-4), respectively, deposited in an amount of 3-7 wt.% n 2 alumina, and the process wire in the presence of air oxygen at a volume ratio of g8xen-1: oxygen 1: (3-6), contact time 0.6 0, 9 c, bulk feed velocity 4000-6000 h 2. The method according to p. 1, I differ u and with the fact that the process wire at a temperature of 530 ° C. 45. The compositions of the catalysts, the conditions of the experiments and the results obtained are shown in Tables 1-3. As can be seen from the table. 1-3, the proposed method allows to increase the yield of benzene from 1-hexene to 71% by weight against 56.3% by weight in a known method. When this conversion hexene-1 90%, benzene selectivity reaches benzene selectivity reaches - 72%. The process does not form other aromatic hydrocarbons, which greatly facilitates the release of benzene, simplifies the whole process technology. Invention Formula 1. A method of producing benzene by dehydro-cyclizing hexene-1 in the presence of a VII catalyst containing a metal oxide of group VI and γ-alumina, at a permeable temperature, of t-, l, and h and y, since use a catalyst containing oxides of chromium (III) and molybdenum (VI) or oxides of molybdenum (VI) and zinc, or oxides of chromium (III) and zinc with an atomic ratio of these metals 1: (0.5-2), respectively, or oxides of chromium (III), molybdenum (VI) and zinc with an atomic ratio of 1: (0.5-2) :( O, 25-4), respectively, deposited in an amount of 3-7 wt.% For 2 alumina, and the process is carried out in the presence of atmospheric oxygen at a volume ratio g8xen-1: oxygen 1: (3-6), contact time 0.6 0, 9 c, bulk feed velocity 4000-6000 h 2. The method according to claim 1, characterized by the fact that the process is carried out at a temperature of 530 ° C. five . Table 1 Note. Reaction conditions: temperature, contact time 0.7 s. CfeH,: Oh, 1: 4, bulk velocity 5100 h tion: temperature, time 1: 4, bulk velocity 5100 h Note Process conditions: catalyst - MoOZ - ZnO,. CrzMo; Zn: 1: 0.5: 2, the amount of active mass is 5 wt.%, The process temperature is 530 C. . Table 3