TH32744A - Method for producing phenol and acetone from cumene - Google Patents

Abstract

DC60 (03/03/41) Phenol and acetone production process consisting of the yield of Oxidizes cumine concentrate to the point that it maintains the content of cubine. And left at least 21 percent by weight, decay, cubic hydroperoxide With sulfuric acid in a medium that is phenol-acetone-cumene Homogeneous in the mixed reactor while keeping the mole ratio of phenol-acetone-cubine at 11: (0.38-0.61) and subsequently decomposition of dicumyl peroxide occurs in flow plug reactors using the mole ratio of phenol-acetone-cumin equal to 1 :(. 1-0.77): (0.35-0.87) at temperatures above 150 ° C with the addition of cumin and the additional cumin content present in the disintegration product will pass through End of the stream By going through the phenol process And went into the process of neutralizing the yield products and a step in which the cumene part was removed with distillation. And circulate some back into Stages of dicumyl peroxide decomposition Increased quantity of cumine Of the output current of the fission results in a better phase separation In the neutralization phase, resulting in less than 20 parts per million of salt and less than 3.5% of the dissolved water, the weight that passes through the end of the stream to Stages of purification The overall process steam consumption was reduced by 0.4-0.6 tonnes / ton of phenol due to the reduced demand for concentrated oxidizing yields and in the removal of water from the fission products. The neutralization stage of the end of the process stream is characterized by high selective reactivity. Low consumption of cumin, 1302-1305 kg / tonne of phenol. In addition, the production of hydroxyacetone and medyl-oxide by-products was reduced. Phenol and azidone production processes, consisting of the Oxidizes cumine concentrate to the point that it maintains the content of cubine. And left at least 21 percent by weight, decay, cubic hydroperoxide With sulfuric acid in a medium that is phenol-acetone-cumene Homogeneous in the mixed reactor while keeping the mole ratio of phenol-acetone-cubine at 1: 1: (0.38-0.61) and subsequently decomposition of dicumyl peroxide occurred in the flow plug reactor using the mole ratio of phenol-acetone-cubine equal to 1. : (1-0.77): (0.35-0.87) at temperatures above 150 ° C with the addition of the cumin and the additional cumin content present in the disintegration product through Towards the end of the stream By going through the phenol process And went into the process of neutralizing the yield products and a step in which the cumene part was removed with distillation. And circulate some back into The process of decomposition of dicumyl percent oxide. Increased quantity of cumine Of the output current of the fission results in a better phase separation In the neutralization phase, resulting in less than 20 parts per million of salt and less than 3.5% of the dissolved water, the weight that passes through the end of the stream to Stages of purification The overall process steam consumption was reduced by 0.4-0.6 tonnes / ton of phenol due to the reduced demand for concentrated oxidizing yields and in the removal of water from the fission products. The neutralization stage of the end-of-process stream is characterized by high selective reactivity. Low consumption of cumin at 1302-1305 kg / tonne of phenol. Also, the production of hydroxyacetone and mecidyl-oxide by-products is reduced:

Claims (9)

1. Optimized process for the production of phenol and acetone by the oxidation of the technical level cumene hydroperoxide (CHP). Catalytic cracking Which is characterized by the oxidizing product to be concentrated up to the cumene content. In cumene hydroperoxide, the technical level is 21 to 30% by weight, and this mixture is used in Catalytic cracking And in the case of fission, the mole ratio of phenol: acetone: cubic at 1: 1 -0.77; 0.35-0.87 is preserved. 2. The process as defined in claim 1, which is characterized by that The process is performed with the technical disintegration of cumene hydroperoxide in the mixed reactor and the disintegration of the by-product dicumyl percides in the reactor. That is a pipe containing The different reaction mediums in the above mentioned reactors. 1 .: (0.38-0.61) 4. The process as defined in claim 2, which is characterized by that For the disintegration of technical level cumene hydroperoxide. In the mixed-reactor, it was preserved depending on the amount of cumine available. At the following ratio (chemical formula) where Gcirc represents the amount of dissolution produced circulating. (Ton / h), GtHPC- The amount of technical CHP fed into the disintegration. (Ton / h) and% cumine - percentage by weight in CHP, technical level. 5. The process set out in claim 2, which is characterized by that Disintegration of dicumil peroxide And dimethyl phenyl carbonol Will be carried out in the reactor Which is a tubular in the reaction medium with the mole ratio of phenol: acetone: cumene equal to 1: (1- 0.77): (0.35-0.87) and is proposed as a temperature equal to 150- 168 ํ C 6. The process set out in claim 5, which is characterized as part Cumine is supplied in an amount not exceeding 160 kg / ton of QMine hydro peroxide. Technical level Into the fission reactor of dicumyl peroxide And dimethyl phenol carbonate 7. The process as set out in claim 5 or 6, which is characterized by the That water is supplied as 1 - 30.4 kg / ton of QMine Hydro Peroxide Technique level. Cal enters the fission reactor of dicumyl peroxide and dimethylphenylcarbinol. 8. Process as defined in Clause 2-7. Which control The process of dissociation of dicumyl peroxide. And dimethyl phenyl carbonol Will occur by Configuration of the ratio Triangle T2 / Triangle T1 in the range of 1.5 to 21.4 where it is proposed as 3 - 8 in the device, where the triangle T2 is the temperature difference of the output at the inlet. And the way out of the phenomenon of Disintegration of dicumil peroxide And dimethyl phenylcarbinol and triangle T1 is the temperature difference of the yield at the inlet. And the exit of the calorimeter, which is installed in the pipeline of the circulation of the product of cumin hydroperoxide disintegration. Technical level 9. The process set out in claim 5, which is characterized as disintegration of dicumyl peroxide. And dimethyl phenyl carbonol Will be carried out in the reactor Which is a conduit in the reaction medium with lower quantities of acetone. Where the lower content of acetone It is taken by the removal of part of the acetone. Or by the help of submission Input of additional quantities of cumine And part of the water goes into the product of the disintegration. Or by using Of both processes 1 0. The process as set out in claim 9, which is characterized by that in Episodes of sulfuric acid neutralization Total volume of cumine and (alpha) - methyl-styrene. In the product of disintegration The supply of hydrocarbon fraction is equal to 40% by weight. The amount of water was 3.6 percent by weight. And the concentration of Salt in the product of disintegration After the phase of sulfuric acid neutralization is 3 to 20 ppm.