CN219209021U

CN219209021U - Tertiary butanol purifying system

Info

Publication number: CN219209021U
Application number: CN202223233313.0U
Authority: CN
Inventors: 周金波; 翟莉慧; 孔祥冰; 张化东; 白云峰; 王艳飞; 马岩; 李金阳; 彭蓉; 薛英芝
Original assignee: Petrochina Co Ltd
Current assignee: Petrochina Co Ltd
Priority date: 2022-11-28
Filing date: 2022-11-28
Publication date: 2023-06-20
Anticipated expiration: 2032-11-28

Abstract

The utility model provides a tertiary butanol purification system, which comprises: the device comprises a first rectifying tower for removing isobutanol in a crude tertiary butanol product, a steam permeation device for removing water and a second rectifying tower for removing methanol, wherein the steam permeation device comprises a pervaporation membrane, a interception side and a permeation side, the top of the first rectifying tower is communicated with the interception side of the steam permeation device, an interception side outlet of the steam permeation device is connected with the second rectifying tower, and a tower kettle of the second rectifying tower is connected with a high-purity tertiary butanol extraction pipeline. The system can separate isobutanol-tertiary butanol, methanol-tertiary butanol and other systems which are difficult to separate, adopts a rectification-steam permeation permeable membrane-rectification coupling technology, is not limited by azeotropy, does not need to add a third component, and can obtain high-purity tertiary butanol.

Description

Tertiary butanol purifying system

Technical Field

The utility model relates to the technical field of tertiary butanol purification, in particular to a tertiary butanol purification system.

Background

Tertiary butanol is widely used in fields of chemical industry, medicine and the like, and 2 kinds of tertiary butanol are commercially available, namely 85% tertiary butanol and anhydrous tertiary butanol (the mass fraction of tertiary butanol is more than 99.5%). The anhydrous tertiary butanol is better in sales condition and is an important fine organic chemical raw material, and the existing tertiary butanol purification method comprises extractive distillation, azeotropic distillation, pervaporation membrane method, adsorption method and the like.

The byproduct tertiary butanol produced in the process of preparing the epoxypropane by the co-oxidation method has relatively high purity, but the co-oxidation process is complex, and the byproduct tertiary butanol also contains components such as water, methanol, isopropanol, isobutanol, 2-butanol and the like.

CN101372442a discloses a device and a method for separating tert-butanol and water by batch distillation and pervaporation, the device for separating tert-butanol and water comprising: the device comprises a rectifying tower body, a rectifying tower kettle, a condenser, a membrane separator, a water jet pump, a condensate storage tank and a circulating pump. The utility model is suitable for a tertiary butanol-water system with simple components, and is not suitable for purifying the byproduct tertiary butanol of a complex system.

CN103071307a discloses a rectification-vapor permeation coupled organic solvent dehydration method and device, wherein the device comprises a raw material tank, a raw material pump, a preheater, a rectification tower and a vapor permeation device which are connected in sequence, and the top of the rectification tower is directly connected with the vapor permeation device. The utility model is suitable for dehydration of organic solvent with single component, and is not suitable for dehydration and purification of tert-butanol which is a byproduct of a complex system containing methanol and isobutanol.

Because the tertiary butanol-water, the isobutanol-tertiary butanol and the methanol-tertiary butanol are difficult to separate, the purification of the byproduct tertiary butanol of the propylene oxide produced by the co-oxidation method is difficult.

Disclosure of Invention

The utility model aims to provide a tertiary butanol purification system, which solves the defect that the proposal of the prior art can not purify the byproduct tertiary butanol of propylene oxide produced by a co-oxidation method, can separate the systems which are difficult to separate such as isobutanol-tertiary butanol, methanol-tertiary butanol and the like, adopts a rectification-steam permeation permeable membrane-rectification coupling technology, is not limited by azeotropy, does not need to add a third component, and can obtain high-purity tertiary butanol.

To achieve the above object, the present utility model provides a tertiary butanol purification system comprising: the device comprises a first rectifying tower for removing isobutanol in a crude tertiary butanol product, a steam permeation device for removing water and a second rectifying tower for removing methanol, wherein the steam permeation device comprises a pervaporation membrane, a interception side and a permeation side, the top of the first rectifying tower is communicated with the interception side of the steam permeation device, an interception side outlet of the steam permeation device is connected with the second rectifying tower, and a tower kettle of the second rectifying tower is connected with a high-purity tertiary butanol extraction pipeline.

The tertiary butanol purification system is characterized in that the top of the second rectifying tower is connected with a second rectifying tower reflux tank for enabling the tower top distillate to flow back into the second rectifying tower.

According to the tertiary butanol purification system disclosed by the utility model, a condenser is arranged between the top of the second rectifying tower and the reflux tank of the second rectifying tower.

According to the tertiary butanol purification system disclosed by the utility model, the top of the first rectifying tower is provided with a reflux branch line.

According to the tertiary butanol purification system disclosed by the utility model, a side line extraction pipeline is arranged on the body of the second rectifying tower.

The tert-butyl alcohol purification system provided by the utility model is characterized in that the pervaporation membrane is one selected from a molecular sieve membrane, a chitosan membrane, a PVA membrane, a sodium alginate membrane and a polyion compound membrane material based on polyacrylic acid.

The tert-butyl alcohol purification system provided by the utility model is characterized in that the pervaporation membrane is a molecular sieve membrane.

The utility model has the beneficial effects that:

1. the tertiary butanol refining system using tertiary butanol as a byproduct in the production of propylene oxide by a co-oxidation method is provided, and a device is provided for a system which is difficult to separate, such as tertiary butanol-water, isobutanol-tertiary butanol, methanol, tertiary butanol and the like, because of the nature of the raw materials, so that the purity of the tertiary butanol reaches more than 99.5%.

2. The vacuum system is adopted, no other solvent is introduced, the operation is convenient, the energy consumption is low, and the byproduct tert-butyl alcohol of propylene oxide can be fully utilized.

Drawings

FIG. 1 is a schematic illustration of a process flow of a tertiary butanol purification system according to the present utility model;

FIG. 2 is a schematic diagram of another process flow of the tertiary butanol purification system of the present utility model.

Wherein, the reference numerals:

1-isobutanol removal unit, 2-dehydration unit, 3-methanol removal unit, 11-first rectifying tower, 21-vapor permeation device, 31-second rectifying tower and 32-reflux tank.

Detailed Description

The following detailed description, given in conjunction with the accompanying drawings, describes the utility model in detail, but is not intended to limit the utility model.

As shown in FIG. 1, the tertiary butanol purification system provided by the utility model comprises an isobutanol removal unit, a dehydration unit and a methanol removal unit; the isobutanol removing unit comprises a first rectifying tower for removing isobutanol in the crude tertiary butanol product, the dehydration unit comprises a steam permeation device for removing water, and the methanol removing unit comprises a second rectifying tower for removing methanol. The vapor permeation device comprises a pervaporation membrane, a interception side and a permeation side, the top of the first rectifying tower is communicated with the interception side of the vapor permeation device, an interception side outlet of the vapor permeation device is connected with the second rectifying tower, and a high-purity tertiary butanol extraction pipeline is connected with the tower bottom of the second rectifying tower.

The tert-butyl alcohol raw material of the byproduct of the production of propylene oxide by the co-oxidation method firstly enters a first rectifying tower 11 for isobutanol-tert-butyl alcohol separation, isobutanol materials are extracted from the tower bottom of the first rectifying tower, the materials which are extracted from the gas phase at the top of the first rectifying tower and are used for removing isobutanol enter a vapor permeation device 21 for dehydration, the vapor partial pressure of water in the other side of the membrane is smaller than the saturated vapor pressure of the water, water molecules continuously permeate through the membrane by means of the difference of the vapor partial pressures formed at the two sides of the membrane, water materials are obtained after condensation at the permeation side, tert-butyl alcohol materials which are used for removing most of water are obtained after condensation at the interception side, the dehydrated tert-butyl alcohol materials at the interception side enter a second rectifying tower 31 for separation, and the high-purity tert-butyl alcohol is extracted from the tower bottom of the second rectifying tower. In a preferred embodiment, the second rectification column has a tray number of 30, and the stream exiting the cut-off side is fed at 14, 16 or 18 stages.

In a specific embodiment of the utility model, a second rectifying tower reflux tank for returning the overhead distillate into the second rectifying tower is connected to the top of the second rectifying tower, and a part of methanol, water and a small amount of tertiary butanol which are the overhead products of the second rectifying tower are used for reflux, and a part of methanol, water and a small amount of tertiary butanol are extracted. In a preferred embodiment, a condenser is arranged between the top of the second rectifying tower and the reflux drum of the second rectifying tower.

In one specific embodiment of the utility model, the top of the first rectifying tower is provided with a reflux branch line, and a part of the material which is extracted from the gas phase at the top of the first rectifying tower and is used for removing the isobutanol is directly connected with a vapor permeation device; a portion is directly connected to the condenser for reflux.

In an embodiment of the present utility model, as shown in fig. 2, a side-draw line is arranged on the second rectifying tower body, so that the purity of the tertiary butanol is better, and the color is better.

In the present utility model, the first rectifying tower, the vapor permeation device and the second rectifying tower condenser are all common devices in the field, and the present utility model is not particularly limited.

In the present utility model, the pervaporation membrane for the vapor permeation mechanism 21 is a commercial water permeable membrane. The water permeable membrane is selected from one of a molecular sieve membrane, a chitosan membrane, a PVA membrane, a sodium alginate membrane or a polyion compound membrane material based on polyacrylic acid, and is preferably a molecular sieve membrane.

Of course, the present utility model is capable of other various embodiments and its several details are capable of modification and variation in light of the present utility model by one skilled in the art without departing from the spirit and scope of the utility model as defined in the appended claims.

Claims

1. A tertiary butanol purification system comprising: the device comprises a first rectifying tower for removing isobutanol in a crude tertiary butanol product, a steam permeation device for removing water and a second rectifying tower for removing methanol, wherein the steam permeation device comprises a pervaporation membrane, a interception side and a permeation side, the top of the first rectifying tower is communicated with the interception side of the steam permeation device, an interception side outlet of the steam permeation device is connected with the second rectifying tower, and a tower kettle of the second rectifying tower is connected with a high-purity tertiary butanol extraction pipeline.

2. The tert-butanol purification system of claim 1, wherein a second rectifying column reflux drum for refluxing an overhead into the second rectifying column is connected to the top of the second rectifying column.

3. The tert-butanol purification system according to claim 2, wherein a condenser is provided between the top of the second rectifying column and the reflux drum of the second rectifying column.

4. The tert-butanol purification system of claim 1, wherein the first rectifying column top is provided with a reflux branch.

5. The tertiary butanol purification system of claim 1, wherein the second rectifying column body is provided with a side draw line.

6. The tertiary butanol purification system of claim 1, wherein the pervaporation membrane is selected from the group consisting of a molecular sieve membrane, a chitosan membrane, a PVA membrane, a sodium alginate membrane, and a polyacrylic acid based polyionic compound membrane material.

7. The tert-butanol purification system of claim 1, wherein the pervaporation membrane is a molecular sieve membrane.