RU2000292C1 - Method of extracting and purifying of secondary butyl alcohol - Google Patents

Abstract

Usage: basic organic synthesis. SUMMARY OF THE INVENTION: The product is secondary butyl alcohol, B F. CsNuO, concentration of 70%. Method for isolating co-CiOHi in Hume, Mio liquid.,.,. TBC dehydration couplings were sent to a rectification reactor, in the upper part of which a layer of ion-exchange catalyst was placed. The process of concentration and purification of WBS is carried out at a top temperature of 85 -90PS and a temperature of a cube of the reactor of 95 11P ° C at a pressure of 0.01-0.02 MPa 1 table

Description

The invention relates to the field of petrochemistry, and in particular to methods for the isolation of secondary butyl alcohol from the liquid products of the dehydration reaction of tertiary butyl alcohol to isobutylene.

A known method for the separation of secondary butyl alcohol (TBL) from products after tertiary butyl alcohol (TBS) dehydration reactors in isobutylene by settling in a tank with the subsequent withdrawal of the upper layer of TBL. However, the use of this method for the isolation of CHD is associated with a number of disadvantages.

before feeding into the tank the mixture of WBS with TBS must be cooled:

complete withdrawal of IWS from the system is difficult and entails large volumes of wastewater, loss of IWS, while IWS is obtained in the form of a solution with a low concentration;

in connection with the formation of a triple azeotrope (VBS, TBS, water), it is impossible to purify VBS by simple rectification; VBS with a concentration of 10–20% is obtained.

The purpose of the invention is to obtain marketable products and to increase the degree of purity.

The goal is achieved. that liquid VHD dehydration products. TBS, water from the bottom of the TBS dehydration reactor to isobutylene is fed to the column-type rectifier reactor, in the upper part of which there is a layer of ion-exchange catalyst. The process of concentration and purification of WBC is carried out at the top of the reactor and the temperature of the reactor cube 95-110 ° C, at a pressure of 0.01-0.02 MPa. Purification of WBC from TBS occurs due to the decomposition of the latter on the catalyst in the indicated mode.

The claimed method is as follows

The rectification reactor has 23 valve plates. Instead of the upper plate, a grid with a grid is mounted. An ion-exchange catalyst is poured onto the grid, which simultaneously acts as a nozzle. VBS and TBS pairs pass from below through the catalyst layer. The temperature of the lysatopate layer is 35–90 ° C, with more reaction70

WITH

U O O O

yu yu

about

jn i, r g ,, inn GBS decomposes into isobuti- .. "., HL-- and P -DE

m from butipene, the air force and water from the top, r-iv .., i through;. dig into the condenser, cooling.:. n i1 and iodoch Azeotropic mixture of the air force with J-IOH gekg0101 to the reflux tank, from where - u, orof the catalytic bed is fed for irrigation, the part of the air force is pumped to the consumer with a concentration of / 071 as a marketable product in terms of the level in the tank. Isobutylene g c drops R is separable, from where the isobu- i img-n pairs are fed to the compressor inlet. Water r iyho relax returns to the process.

P) and m r 1 The apparatus represents the t, nf.nfi i-olonpu from f: i. X1BH10T, with a height of g m and an inner diameter of 1200 mm — 23 tr. 1 measure of styrene with divinylbenzene and 30 l. h of poprippilene catalyst with a t i i a-exchange capacity of 2.9 s -kn / h g; , wow catalyst bulk. . g v gs k.a D pi 1 l fr.h About 45 g / ml

And pigcnio colonies feed the mixture into colioglps 1000 xg / and containing 15% BF-C. 57--1; C-7P 7o pods 27-- non-identifiable - R zhamchich primgs

Tnr inpp, i p, i columns 88 C, cube

K (.. / avrnie in the column 0.015 MPe

Fl i M - POR number 5 Get 600 t / year Air Force

with a concentration of 70% containing 2% TBS

and 27% water

Water from the cube of the column is returned to the process.

EXAMPLE 2 The experiment was carried out similarly to that described in Example 1. Only KU-23 catalyst was loaded into the apparatus.

The catalyst has a static exchange capacity of 4.1 mEq / h of dry catalyst.

The process is carried out as described in Example 1,

Obtained from the top of the air force column has a concentration of 70% 1% TBS, the rest is water.

The results of the experiments are tabulated.

The table shows that the proposed method for the separation of the Air Force allows to achieve an increase in the yield of the Air Force and a decrease in the concentration of tertiary butyl alcohol through the use of the ion exchange catalyst KU-2FPP and KU-23

Claims (1)

The claims A method for the isolation and purification of secondary butyl alcohol from liquid products of dehydration of tertiary butyl alcohol to isobutylene, characterized in that, in order to obtain marketable products and increase the degree of their frequency, liquid products of dehydration of tertiary butyl distillation in a column-type distillation reactor to the top part of which the ion-exchange catalyst is placed and supported; top temperature 85-90 ° С, cube 95 100PS and pressure 0.01-0.002 MPa