CN207512105U - A kind of hexamethylene diamine distillation system - Google Patents
A kind of hexamethylene diamine distillation system Download PDFInfo
- Publication number
- CN207512105U CN207512105U CN201721441932.5U CN201721441932U CN207512105U CN 207512105 U CN207512105 U CN 207512105U CN 201721441932 U CN201721441932 U CN 201721441932U CN 207512105 U CN207512105 U CN 207512105U
- Authority
- CN
- China
- Prior art keywords
- reaction tower
- hexamethylene diamine
- reaction
- tower
- distillation system
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a kind of hexamethylene diamine distillation system, including：Preceding process reaction unit, first reaction tower, second reaction tower, heat exchanger, second reaction tower reboiler, second reaction tower relays slot, second reaction tower overhead condenser, second reaction tower steam jet pump, process reaction unit afterwards, wherein, first reaction tower, it is connected between second reaction tower by heat exchanger, it is connected between the preceding process reaction unit and the first reaction tower, the rear process reaction unit and the second reaction tower, it is connected between second reaction tower reboiler, the second reaction tower overhead condenser is located at the top with the second reaction tower, the second reaction tower relaying slot and the second reaction tower overhead condenser, it is connected between second reaction tower.By the above-mentioned means, hexamethylene diamine distillation system provided by the utility model, by transformation, below 30PPm is dropped to by the content of the light components impurity such as azepan, the γ aminopropanols in thick hexamethylene diamine.
Description
Technical field
The utility model is related to a kind of hexamethylene diamine technique, more particularly to azepan, gamma-amino third in thick hexamethylene diamine
The removing means of the light components impurity such as alcohol belongs to chemical technology field.
Background technology
In existing adipic dinitrile hydrogenation production hexamethylene diamine technique, azepan, gamma-amino propyl alcohol etc. are used as light component impurity
Presence, thick hexamethylene diamine purification produce smart hexamethylene diamine during, with the removing of other impurity, azepan, gamma-amino
Propyl alcohol directly affects the quality-improving of hexamethylene diamine product, the removal methods of the light components impurity such as azepan, gamma-amino propyl alcohol
Mainly rectifying removal method.
Rectifying removal method：Thick hexamethylene diamine enters after distillation system by a series of rectifying, impurity by separation removal, due to
The light components impurity such as azepan, gamma-amino propyl alcohol not only directly affect the quality of hexamethylene diamine in the product, and to downstream
The product quality of hexamethylene diamine user is also most important, thus we provide it is a kind of can be the azepine cycloheptyl in hexamethylene diamine
The light components impurity contents such as alkane, gamma-amino propyl alcohol drop to the production method of below 30PPm.
Utility model content
The utility model mainly solving the technical problems that how to provide in a kind of thick hexamethylene diamine remove azepan,
The system of the impurity such as gamma-amino propyl alcohol, by containing for the light components impurity such as azepan, the gamma-amino propyl alcohol in thick hexamethylene diamine
Amount drops to below 30PPm.
In order to solve the above technical problems, the technical solution that the utility model uses is：A kind of hexamethylene diamine rectifying is provided
System, including：Preceding process reaction unit, the first reaction tower, the second reaction tower, heat exchanger, the second reaction tower reboiler, second are instead
Tower relaying slot, the second reaction tower overhead condenser, the second reaction tower steam jet pump, rear process reaction unit are answered, wherein, it is described
The first reaction tower, connected by heat exchanger between the second reaction tower, the preceding process reaction unit and the first reaction tower it
Between be connected, the rear process reaction unit is connected between reacting tower reboiler with the second reaction tower, second, described
Two reaction tower overhead condensers are located at the top with the second reaction tower, and the second reaction tower relaying slot is reacted with second
It is connected between column overhead condenser, the second reaction tower, the second reaction tower relaying slot is located at the second reaction tower overhead condensation
Between device, the second reaction tower, it is connected between the second reaction tower steam jet pump and the second reaction tower overhead condenser.
In a preferred embodiment, the hexamethylene diamine distillation system also include the first reaction tower overhead condenser,
First reaction tower relaying slot, the first reaction tower reboiler, the first reaction tower overhead condenser are located at the first reaction tower
Top, and be connected with the first reaction tower relaying slot, it is connected between the described first reaction tower reboiler and the first reaction tower.
In a preferred embodiment, the hexamethylene diamine distillation system also includes the second reaction tower head tank, described
Second reaction tower head tank one end react tower reboiler with the first reaction tower, first and be respectively connected with, the other end and heat exchanger
Between be connected.
In a preferred embodiment, the hexamethylene diamine distillation system, which also includes, arranges relaying slot outside the first reaction tower,
It arranges outside first reaction tower and is connected respectively between relaying slot and the first reaction tower, the first reaction tower relaying slot.
In a preferred embodiment, the hexamethylene diamine distillation system also includes the first reaction tower steam jet pump,
It is connected between the first reaction tower steam jet pump and the first reaction tower overhead condenser.
In a preferred embodiment, the hexamethylene diamine distillation system also includes to connect the first reaction tower, the
The line device of two reaction towers, the line device is between first reaction tower, the second reaction tower.
The beneficial effects of the utility model are：By transformation, azepan, the gamma-amino that will contain in thick hexamethylene diamine
The light components impurity such as propyl alcohol, by carrying out first time distillation and the second reaction tower negative pressure in the first reaction tower negative pressure rectifying column
The secondary rectifying of rectifying column drops to the light components impurity contents such as azepan, the gamma-amino propyl alcohol in hexamethylene diamine product
Below 30PPm.
Description of the drawings
It is required in being described below to embodiment in order to illustrate more clearly of the technical scheme in the embodiment of the utility model
Attached drawing to be used is briefly described, it should be apparent that, the accompanying drawings in the following description is only some realities of the utility model
Example is applied, it for those of ordinary skill in the art, without creative efforts, can also be according to these attached drawings
Other attached drawings are obtained, wherein：
Fig. 1 is the structure diagram of one specific embodiment of the utility model hexamethylene diamine distillation system.
Specific embodiment
Below by the technical scheme in the utility model embodiment is clearly and completely described, it is clear that described
Embodiment is only the part of the embodiment of the utility model, instead of all the embodiments.Based on the implementation in the utility model
Example, all other embodiment that those of ordinary skill in the art are obtained without making creative work belong to
The range of the utility model protection.
Referring to Fig. 1, a kind of hexamethylene diamine distillation system is provided in a specific embodiment of the utility model, it is described
Hexamethylene diamine distillation system includes：First reaction tower overhead condenser 2, the first reaction tower relaying slot 3, first react tower reboiler 4,
Preceding process reaction unit 12, the first reaction tower 1, the second reaction tower 7, heat exchanger 6, second react tower reboiler 8, the second reaction tower
Slot 9, the second reaction tower overhead condenser 10, the second reaction tower steam jet pump 14, rear process reaction unit 11 are relayed, wherein,
The first reaction tower overhead condenser 2 is located at the top of the first reaction tower 1, and is connected with the first reaction tower relaying slot 3,
It is connected between the first reaction tower reboiler 4 and the first reaction tower 1.First reaction tower 1, the second reaction tower 7
Between connected by heat exchanger 6, be connected between the preceding process reaction unit 12 and the first reaction tower 1, the rear work
Sequence reaction unit 11 is connected between reacting tower reboiler 8 with the second reaction tower 7, second, and the described second reaction column overhead is cold
Condenser 10 is located at the top with the second reaction tower 7, and second reaction tower relays 9 and second reaction tower overhead condensation of slot
It is connected between device 10, the second reaction tower 7, second reaction tower relaying slot 9 is located at the second reaction tower overhead condenser 10, the
Between two reaction towers 7, it is connected between the second reaction tower steam jet pump 14 and the second reaction tower overhead condenser 10.
The hexamethylene diamine distillation system, which also includes, arranges relaying slot 16 outside the second reaction tower head tank 5, the first reaction tower
With the first reaction tower steam jet pump 13, described 5 one end of the second reaction tower head tank and the first reaction tower 1, the first reaction tower
Reboiler 4 is respectively connected with, and is connected between the other end and heat exchanger 6.Relaying slot 16 and the are arranged outside first reaction tower
It is connected respectively between one reaction tower 1, the first reaction tower relaying slot 3.The first reaction tower steam jet pump 13 and first is anti-
It answers and is connected between column overhead condenser 2.
The hexamethylene diamine distillation system also includes the line device for connecting the first reaction tower 1, the second reaction tower 7
15, the line device 15 is between first reaction tower 1, the second reaction tower 7.
In a specific embodiment, the hexamethylene diamine distillation system includes：
1# towers：Using negative pressure rectifying, tower top steam jet pump takes out negative pressure to tower；Top vacuum pressure is maintained at 60-
100mmHg or so is condensed in tower top with steam state extraction section material, containing a large amount of fusing points less than hexamethylene diamine in this material
The light components impurity such as azepan, gamma-amino propyl alcohol.For the hexamethylene diamine that efficiently produces choice goods, a material part for extraction passes through
Cross relaying slot discharge, another part by conveying equipment conveying flows back into tower top recycle, into tower top a material part to
Bottom of towe flows.Divide four sections in tower to be filled with High Efficient Standard Packing, be effectively increased the residence time of liquid in tower and be evenly distributed, make
Lower melting-point material is sufficiently separated with hexamethylene diamine, be less than hexamethylene diamine so as to fusing point in the thick hexamethylene diamine of efficient removal light group
Divide impurity.One is set with middle pressure steam in 1# tower bottom of towe（Pressure 1.2-1.5MPaG）Reboiler for heat source is that 1# tower materials add
The thick hexamethylene diamine for being stripped of most light component impurity is sent into the head tank of 2# towers by heat, tower bottom liquid conveying equipment.First
The overwhelming majority of secondary removing light component impurity, it is miscellaneous effectively to reduce the light components such as azepan in thick hexamethylene diamine, gamma-amino propyl alcohol
The content of matter.
2# towers：2# towers have removed part tower tray, use filler of the ripple silk net as filling instead, are divided into three sections of fillings（Filler
Highly it is respectively 4.1 meters, 4.1 meters, 4.0 meters）.Material in the head tank of 2# towers is sent into liquid delivery pump in a heat exchanger
It is preheated, material is heated to 100 DEG C or more feeding 2# towers.2# towers are equally using negative pressure rectifying, tower top steam jet pump
Negative pressure is taken out to tower.Top vacuum pressure is maintained at 70-100mmHg or so, is condensed in tower top with steam state extraction section material,
Containing a small amount of fusing point less than light components impurity such as azepan, the gamma-amino propyl alcohol of hexamethylene diamine in this material.In order to efficiently give birth to
Fine work hexamethylene diamine is produced, the material of part extraction delivers into tower top with equipment for liquid transportation by relaying slot and recycles, another part
Pass through pipelined to 1# tower tops imurity-removal again；The material part for being recycled into tower top is flowed to bottom of towe, three sections in tower
The filler filled with ripple silk net, is effectively increased different medium swap time and fluid distrbution in tower, makes lower melting-point material
It is sufficiently separated with hexamethylene diamine, so as to which fusing point is less than the light component impurity of hexamethylene diamine in the thick hexamethylene diamine of efficient removal.To passing through 1# towers
The hexamethylene diamine of removing light component impurity carries out the removing of light component impurity again, makes azepan, gamma-amino in thick hexamethylene diamine
The content of the light components impurity such as propyl alcohol drops to below 30PPm.One is set with middle pressure steam in 2# tower bottom of towe（Pressure 1.2-
1.5MPaG）Reboiler for heat source is the heating of 2# towers material, and bottom liquid, which conveys to be pumped into subsequent fine and evaporate equipment, removes other
Impurity.
Likewise, in another specific embodiment, the hexamethylene diamine distillation system includes：
1# towers：Using negative pressure rectifying, tower top steam jet pump takes out negative pressure to tower；Top vacuum pressure is maintained at 60-
100mmHg or so.Thick hexamethylene diamine material from preceding process enters 1# towers 1.It is cold with the progress of steam state extraction section material in tower top
It is solidifying, containing a large amount of fusing points less than light components impurity such as azepan, the gamma-amino propyl alcohol of hexamethylene diamine in this material, for height
The hexamethylene diamine that produces choice goods is imitated, for a material part for extraction by relaying slot discharge, another part conveys reflux by conveying equipment
It recycles into tower top, is flowed into a material part for tower top to bottom of towe, divide four sections in tower and filled with High Efficient Standard Packing, effectively
Increase different medium swap time and fluid distrbution in tower, lower melting-point material is made to be sufficiently separated with hexamethylene diamine, so as to
Fusing point is less than the light component impurity of hexamethylene diamine in the thick hexamethylene diamine of efficient removal.One is set with middle pressure steam in 1# tower bottom of towe（Pressure
1.2-1.5MPaG）Reboiler for heat source is the heating of 1# towers, and it is miscellaneous that tower bottom liquid conveying equipment will be stripped of most light components
The thick hexamethylene diamine of matter is sent into the head tank of 2# towers.The overwhelming majority of light component impurity is removed for the first time, effectively reduces thick hexamethylene diamine
The content of the light components impurity such as middle azepan, gamma-amino propyl alcohol.
2# towers：Material in the head tank of 2# towers, which is sent into liquid delivery pump in a heat exchanger, to be preheated, material quilt
It is heated to 100 DEG C or more feeding 2# towers.2# towers use negative pressure rectifying, and tower top steam jet pump takes out negative pressure to 2# towers.Tower top is true
Pneumatics power is maintained at 70-100mmHg or so, is condensed in tower top with steam state extraction section material, containing a small amount of in this material
Fusing point is less than light components impurity such as azepan, the gamma-amino propyl alcohol of hexamethylene diamine, for the hexamethylene diamine that efficiently produces choice goods, portion
The material of extraction is divided to deliver into overhead reflux with equipment for liquid transportation by relaying slot, another part passes through pipelined to 1#
Tower top imurity-removal again.The material part for being recycled into tower top is flowed to bottom of towe, is divided four sections in tower and is filled with ripple silk net
Filler, be effectively increased different medium swap time and fluid distrbution in tower, lower melting-point material made fully to divide with hexamethylene diamine
From so as to which fusing point is less than the light component impurity of hexamethylene diamine in the thick hexamethylene diamine of efficient removal.To removing light component impurity by 1# towers
Hexamethylene diamine carry out the removing of light component impurity again, make the light components such as azepan in thick hexamethylene diamine, gamma-amino propyl alcohol miscellaneous
The content of matter drops to below 30PPm.One is set with middle pressure steam in 2# tower bottom of towe（Pressure 1.2-1.5MPaG）For boiling again for heat source
Device is heated for 2# towers, and bottom liquid conveying is pumped into subsequent fine and evaporates the other impurity of equipment removing.
Therefore, the utility model has the following advantages：By transformation, by the azepan contained in thick hexamethylene diamine, γ-
The light components impurity such as aminopropanol, by carrying out the secondary of first time distillation and 2# negative pressure rectifying columns in 1# negative pressure rectifying columns
The light components impurity contents such as azepan, the gamma-amino propyl alcohol in hexamethylene diamine are dropped to below 30PPm by rectifying.
The above description is only the embodiments of the present invention, and it does not limit the scope of the patent of the present invention, every
The equivalent structure or equivalent flow shift made using the utility model description is directly or indirectly used in other phases
The technical field of pass, is equally included in the patent within the scope of the utility model.
Claims (6)
1. a kind of hexamethylene diamine distillation system, which is characterized in that including：Preceding process reaction unit（12）, the first reaction tower（1）,
Two reaction towers（7）, heat exchanger（6）, second reaction tower reboiler（8）, the second reaction tower relaying slot（9）, second reaction column overhead
Condenser（10）, the second reaction tower steam jet pump（14）, rear process reaction unit（11）, wherein, first reaction tower
（1）, the second reaction tower（7）Between pass through heat exchanger（6）Connection, the preceding process reaction unit（12）With the first reaction tower
（1）Between be connected, the rear process reaction unit（11）With the second reaction tower（7）, second reaction tower reboiler（8）Between
It is connected, the second reaction tower overhead condenser（10）Positioned at described with the second reaction tower（7）Top, described second
Reaction tower relays slot（9）With the second reaction tower overhead condenser（10）, the second reaction tower（7）Between be connected, described second is anti-
Tower is answered to relay slot（9）Positioned at the second reaction tower overhead condenser（10）, the second reaction tower（7）Between, second reaction tower
Steam jet pump（14）With the second reaction tower overhead condenser（10）Between be connected.
2. hexamethylene diamine distillation system according to claim 1, which is characterized in that the hexamethylene diamine distillation system also includes
There is the first reaction tower overhead condenser（2）, the first reaction tower relaying slot（3）, first reaction tower reboiler（4）, described first
Reaction tower overhead condenser（2）Positioned at the first reaction tower（1）Top, and with the first reaction tower relay slot（3）It is connected, it is described
First reaction tower reboiler（4）With the first reaction tower（1）Between be connected.
3. hexamethylene diamine distillation system according to claim 2, which is characterized in that the hexamethylene diamine distillation system also includes
There is the second reaction tower head tank（5）, the second reaction tower head tank（5）One end and the first reaction tower（1）, the first reaction tower
Reboiler（4）It is respectively connected with, the other end and heat exchanger（6）Between be connected.
4. hexamethylene diamine distillation system according to claim 2, which is characterized in that the hexamethylene diamine distillation system also includes
Have and relaying slot is arranged outside the first reaction tower（16）, first reaction tower is arranged outside relays slot（16）With the first reaction tower（1）, first
Reaction tower relays slot（3）Between connect respectively.
5. hexamethylene diamine distillation system according to claim 2, which is characterized in that the hexamethylene diamine distillation system also includes
There is the first reaction tower steam jet pump（13）, the first reaction tower steam jet pump（13）With the first reaction tower overhead condensation
Device（2）Between be connected.
6. hexamethylene diamine distillation system according to claim 1, which is characterized in that the hexamethylene diamine distillation system also includes
It is useful for the first reaction tower of connection（1）, the second reaction tower（7）Line device（15）, the line device（15）Positioned at institute
The first reaction tower stated（1）, the second reaction tower（7）Between.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721441932.5U CN207512105U (en) | 2017-11-02 | 2017-11-02 | A kind of hexamethylene diamine distillation system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721441932.5U CN207512105U (en) | 2017-11-02 | 2017-11-02 | A kind of hexamethylene diamine distillation system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN207512105U true CN207512105U (en) | 2018-06-19 |
Family
ID=62537010
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201721441932.5U Active CN207512105U (en) | 2017-11-02 | 2017-11-02 | A kind of hexamethylene diamine distillation system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN207512105U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109438256A (en) * | 2018-11-13 | 2019-03-08 | 中国化学赛鼎宁波工程有限公司 | A kind of production method and production system of hexamethylene diamine |
-
2017
- 2017-11-02 CN CN201721441932.5U patent/CN207512105U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109438256A (en) * | 2018-11-13 | 2019-03-08 | 中国化学赛鼎宁波工程有限公司 | A kind of production method and production system of hexamethylene diamine |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110282676B (en) | Hydrazine hydrate wastewater evaporation crystallization equipment and evaporation crystallization process thereof | |
| US4601790A (en) | Process for deodorizing and/or physical refining of cocoa butter and cocoa butter substitutes | |
| CN105237369B (en) | A kind of method of isoborneol dehydrogenation Gum Camphor and equipment thereof | |
| CN207512105U (en) | A kind of hexamethylene diamine distillation system | |
| CN107073353A (en) | The improvement related to oxirane recovery | |
| CN106631699A (en) | Method for preparing sec-butyl alcohol | |
| CN109053492A (en) | A kind of adiponitrile rectifying and purifying system and its rectification and purification method | |
| CN102391064B (en) | Process for recovering and refining extracting agent in production procedure of hexanolactam | |
| BR112019018494B1 (en) | METHOD OF REMOVING AN AROMATIC AMINE, METHOD OF PREPARING AN AQUEOUS LEUKOINDIGO SOLUTION, STABLE AQUEOUS LEUKOINDIGO SOLUTION AND METHOD OF PRODUCING INDIGO | |
| CN110818900B (en) | Method and production system for continuously catalyzing, synthesizing and separating high-purity low-viscosity dimethyl silicone oil | |
| KR101674655B1 (en) | Benzene Removal Equipment and Removal Method in Gasoline Blend from Fluidized Catalytic Cracker Reformate | |
| CN101255122A (en) | Method for purifying dimethylacetamide from spinning wastewater | |
| CN103772185A (en) | Device and method for removing moisture and heteroacids in acetic acid | |
| CN107311871A (en) | The process for separation and purification of monomethyl amine diformazan amine blends in a kind of synthetic methylamine system | |
| TWI828051B (en) | Process for the energy-efficient production of alkali metal alkoxides | |
| CN107162875A (en) | A kind of technique and system that refined methanol and absolute ethyl alcohol are extracted from crude carbinol | |
| CN202246490U (en) | Peach aldehyde continuous reaction device | |
| CN106957284A (en) | A kind of separating-purifying process for refining of tertiary carbonic acid glycidyl ester crude product | |
| CN109485548A (en) | A kind of method and device hydrolyzing preparation and separation sec-butyl alcohol by sec-butyl acetate | |
| CN102503915B (en) | Peach aldehyde continuous reaction device | |
| CN207294646U (en) | A kind of process units of methyl tertiary butyl ether(MTBE) | |
| CN105585504B (en) | Liquid ammonia process for caustic soda purification produces ethylenediamine technique | |
| CN206986063U (en) | A kind of system that refined methanol and absolute ethyl alcohol are extracted from crude carbinol | |
| CN206045453U (en) | A kind of efficient Distallation systm of propane diamine crude product | |
| CN115215894B (en) | Preparation method of low-acid-value tetramethyl dihydro disiloxane |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |