Continuous production system of nano disperse dyes

A nano-dispersion and production system technology, applied in the direction of organic dyes, azo dyes, monoazo dyes, etc., can solve the problems of large differences in dye batches, inconvenient application of post-treatment agents, and large particle sizes of dyes

Active Publication Date: 2021-04-02
BEIJING UNIV OF CHEM TECH
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  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

In industrial production, azo disperse dyes are usually carried out in batch operation in stirred tank reactors. Due to the complexity of the synthesis process of azo dyes and the limitation of the volume of the stirred tank itself, it is difficult to achieve uniform mixing between materials, resulting in dyes The decline in productivity and the large difference between batches of dyes bring inconvenience to the application of post-treatment agents for dyes
Moreover, the particle size of the dye particles synthesized in the stirred tank reactor is relatively large and cannot be directly used for dyeing.

Method used

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  • Continuous production system of nano disperse dyes
  • Continuous production system of nano disperse dyes
  • Continuous production system of nano disperse dyes

Examples

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example 1

[0082] Example 1 A kind of continuous production of azo nano-disperse dyes

[0083] In this embodiment, the diazo component includes p-nitroaniline and nitrite, the diazotization reagent includes hydrochloric acid, and the coupling component includes N-ethyl-N-cyanoethylaniline and acetic acid.

[0084] The diazotization reaction process is: premix the p-nitroaniline and nitrite mixture with hydrochloric acid solution through the premixing component, such as figure 2 shown, and then continuously fed into the spiral coil reactor through the pipeline to obtain the diazonium salt solution or suspension. The diazotization reaction is carried out at -5°C to 30°C, preferably 5°C to 10°C. The molar ratio of hydrogen ions of diazotization reaction hydrochloric acid to p-nitroaniline is Preferably 2.8:1, the molar ratio of sodium nitrite to p-nitroaniline is 1-2:1, preferably 1.07:1, and the feed flow rate is 50-300mL / min, preferably 50-120mL / min.

[0085] The coupling reaction pro...

example 2

[0094] A kind of continuous preparation method of example 2 nanoscale disperse dyes

[0095] In this embodiment, the diazo component includes p-nitroaniline and nitrite, the diazotization reagent includes hydrochloric acid, and the coupling component includes N-ethyl-N-cyanoethylaniline, acetic acid and Dispersant.

[0096] A method for preparing continuous nanometer disperse dyes using supergravity, characterized in that the method comprises the steps of:

[0097] The diazotization reaction process is: premix the p-nitroaniline and nitrite mixture with hydrochloric acid solution through the premixing component, such as figure 2 shown, and then continuously fed into the spiral coil reactor through the pipeline to obtain the diazonium salt solution or suspension. The diazotization reaction is carried out at -5°C to 30°C, preferably 5°C to 10°C. The molar ratio of hydrogen ions of diazotization reaction hydrochloric acid to p-nitroaniline is Preferably 2.8:1, the molar rati...

example 3

[0101] A kind of continuous preparation method of example 3 nanoscale disperse dyes

[0102] In this embodiment, the diazo component includes p-nitroaniline and nitrite, the diazotization reagent includes hydrochloric acid, and the coupling component includes N-ethyl-N-cyanoethylaniline, acetic acid and Dispersant.

[0103] A method for preparing continuous nanometer disperse dyes using supergravity, characterized in that the method comprises the steps of:

[0104] The diazotization reaction process is: premix the p-nitroaniline and nitrite mixture with hydrochloric acid solution through the premixing component, such as figure 2 shown, and then continuously fed into the spiral coil reactor through the pipeline to obtain the diazonium salt solution or suspension. The diazotization reaction is carried out at -5°C to +30°C, preferably 5°C to 10°C. The molar ratio of hydrogen ions of hydrochloric acid to p-nitroaniline in diazotization reaction is Preferably 2.8:1, the molar ...

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Abstract

The invention provides a continuous production system of nano disperse dyes, aiming at the characteristics that disperse dye materials are easy to block and the like, a feed pipe premixing emptying pipeline and an emptying pipeline at an inlet and an outlet of a spiral coil are designed, the emptying pipeline is connected with a diazotization reaction raw material feed port, and an outlet is connected with a supergravity coupling reactor. Due to the fact that a pressure relief emptying pipeline is locally arranged on the emptying pipeline, the emptying pipeline can effectively solve the problem of material feeding blockage, and materials can evenly enter a spiral pipe reactor to be subjected to diazotization reaction.

Description

technical field [0001] The invention relates to the technical field of preparing nanometer disperse dyes. More specifically, it relates to a continuous production system of nanometer disperse dyes. Background technique [0002] Disperse dyes are special dyes for polyester fibers and acetate fibers, and are the dyes with the largest output among all dye varieties in my country. In industrial production, azo disperse dyes are usually carried out in a batch operation mode in a stirred tank reactor. Due to the complexity of the synthesis process of azo dyes and the limitation of the volume of the stirred tank itself, it is difficult to achieve uniform mixing between materials, resulting in dyes The decline in productivity and the large differences between batches of dyes have brought inconvenience to the application of post-treatment agents for dyes. Moreover, the particle size of the dye particles synthesized in the stirred tank reactor is relatively large and cannot be direc...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C09B29/01C09B29/085B01J19/18B01J19/00B01J3/04
CPCC09B29/0007C09B29/08B01J19/0046B01J19/18B01J19/0013B01J3/04B01J2219/00081
Inventor 邹海魁薛云龙孙宝昌初广文陈建峰罗勇张亮亮
Owner BEIJING UNIV OF CHEM TECH
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