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A kind of production process of phenol hydrogenation cyclohexanone

A production process and cyclohexanone technology are applied in the production process field of cyclohexanone, and can solve the problems of complex cyclohexanone production technology, low catalyst utilization rate, low separation efficiency, etc. Convenience and the effect of reducing recycling costs

Active Publication Date: 2016-02-10
NANJING TECH UNIV +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0004] The purpose of the present invention is to provide a one-step process for the production of cyclohexanone by hydrogenation of phenol in order to solve the shortcomings of the existing cyclohexanone production technology, such as complex process, high energy consumption, and low catalyst utilization rate.
It can realize the reuse of catalyst on the basis of highly selective preparation of cyclohexanone, and overcome the problems of low separation efficiency and serious loss of catalyst in traditional methods.

Method used

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  • A kind of production process of phenol hydrogenation cyclohexanone
  • A kind of production process of phenol hydrogenation cyclohexanone
  • A kind of production process of phenol hydrogenation cyclohexanone

Examples

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Embodiment 1

[0017] One end of the membrane is fired and sealed, and the other end is connected to the discharge pipeline with a rubber gasket and a stainless steel nut. The membrane tube uses a pore size of 500nmAl 2 o 3 Ceramic membrane tube, L-shaped membrane module. After the membrane was fixed, 8g of phenol (phenol concentration: 0.11mol / l), 750ml of deionized water, and 7.0g of PdCN catalyst (PdCN / phenol mass ratio: 7:8) were added to the reactor, and the total reaction volume was 765ml. After closing the kettle, exhaust 5 times at a hydrogen pressure of about 0.50MPa, turn on the stirring motor to 200r / min, heat to 80°C, adjust the hydrogen pressure to 0.50MPa, adjust the stirring rate to 500r / min, and start the intermittent reaction. During the reaction, hydrogen was supplemented to 0.50 MPa when the hydrogen pressure dropped from 0.50 MPa to 0.45 MPa. After reacting for 5 hours, discharge the unreacted hydrogen in the reactor, and replace it twice with nitrogen at 0.5 MPa. Coo...

Embodiment 2

[0019] One end of the membrane is fired and sealed, and the other end is connected to the discharge pipeline with a rubber gasket and a stainless steel nut. The membrane tube uses a zirconia membrane with a pore size of 500nm and a horizontal membrane module. After the membrane was fixed, 18g of phenol (phenol concentration: 0.25mol / l), 750ml of methanol, and 2g of PdCN catalyst (PdCN / phenol mass ratio: 1:9) were added to the reactor, and the total reaction volume was 763ml. After closing the kettle, exhaust 5 times at a hydrogen pressure of about 0.5MPa, turn on the stirring motor to 200r / min, heat to 90°C, adjust the hydrogen pressure to 1.0MPa, adjust the stirring rate to 400r / min, and start the intermittent reaction. During the reaction, hydrogen was supplemented to 1.0 MPa when the hydrogen pressure dropped from 1.0 MPa to 0.95 MPa. After reacting for 8 hours, discharge the unreacted hydrogen in the reactor, and replace it twice with nitrogen at 0.5 MPa. Cool down to 30...

Embodiment 3

[0021]One end of the membrane is fired and sealed, and the other end is connected to the discharge pipeline with a rubber gasket and a stainless steel nut. The membrane tube uses a stainless steel membrane tube with a pore size of 100nm and a vertical membrane module. After the membrane was fixed, 34g of phenol (phenol concentration: 0.48mol / l), 715ml of dichloromethane, and 6.8g of PdCN catalyst (PdCN / phenol mass ratio: 1:5) were added to the reactor, and the total reaction volume was 756ml. After closing the kettle, exhaust 5 times at a hydrogen pressure of about 0.5MPa, turn on the stirring motor to 200r / min, heat to 30°C, adjust the hydrogen pressure to 1.0MPa, adjust the stirring rate to 800r / min, and start the intermittent reaction. During the reaction, hydrogen was supplemented to 1.0 MPa when the hydrogen pressure dropped from 1.0 MPa to 0.95 MPa. After reacting for 8 hours, discharge the unreacted hydrogen in the reactor, and replace it twice with nitrogen at 0.5 MPa...

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Abstract

The invention relates to a technology for production of cyclohexanone by phenol hydrogenation. Pd@CN is adopted as the catalyst to prepare cyclohexanone by an intermittent operation mode. The reaction product is subjected to inorganic membrane filtration and collection, and conventional treatment, then the cyclohexanone product can be obtained, and the Pd@CN catalyst is intercepted by the membrane and left in a reaction kettle for repeated use, thus realizing organic combination of production of cyclohexanone from phenol and repeated use of catalyst, simplifying the process, and improving the production efficiency.

Description

technical field [0001] The invention relates to a production process for preparing cyclohexanone, in particular to a production process for preparing cyclohexanone by hydrogenating phenol. Background technique [0002] Cyclohexanone is an important organic chemical raw material, mainly used in the production of caprolactam and adipic acid. They are monomers for the production of nylon 6 and nylon 66, and are also important intermediates for fine chemicals such as dyes, medicines, and coatings. In addition, it can also be used as a solvent, a reagent, and the like. [0003] The production methods of cyclohexanone mainly include cyclohexane oxidation and phenol hydrogenation. The raw material cost of the cyclohexane oxidation method is low, but the contact of cyclohexane with air is easy to cause explosion, and more by-products and waste water are produced during the production process. The reaction conditions are high temperature and high pressure, high energy consumption, a...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C45/51C07C49/403
CPCC07C45/006C07C2601/14C07C49/403
Inventor 陈日志李颖唐文麒张红艳姜红邢卫红
Owner NANJING TECH UNIV