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Methods of Handling Phenols

A fluid and reactor technology, applied in the continuous field of removing hydroxyacetone and methylbenzofuran, can solve the problem of low reaction rate

Active Publication Date: 2011-12-28
INEOS PHENOL & GMBH CO
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

While this one-step process does effectively reduce hydroxyacetone and methylbenzofuran, due to the low reaction rate at this relatively low temperature, the process requires relatively high reactor volumes and / or highly activated ion exchange resin

Method used

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  • Methods of Handling Phenols
  • Methods of Handling Phenols
  • Methods of Handling Phenols

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0061] 1 kg / h of impure phenol stream containing 200 wppm hydroxyacetone was treated on ion exchange resin type K2431 from Lanxess. The plug flow reactor has a diameter of 0.025 m and a height of 1.2 m. The weight hourly space velocity WHSV (tonnes of phenol / hour / m3) in the plug flow reactor was thus 1.7. The temperature was adjusted so that the final concentration of hydroxyacetone after treatment was about 10 wppm. Fresh catalyst and catalyst samples from production units with varying degrees of usage were used. figure 1 The temperature required to compensate for the deactivation associated with the conversion of hydroxyacetone is shown. The activity of a new catalyst can be rated as "1.0". On this new ion exchange resin, a temperature of 70°C was sufficient to convert hydroxyacetone from 200 wppm to 10 wppm. The temperature must be increased to obtain the same conversion on the partially used ion exchange resin. For example, the temperature must be raised to 123°C to ...

Embodiment 2

[0067] First, on the new fixed-bed ion exchange resin CT151 purchased from Purolite, the continuous treatment at 120°C was used figure 2 The impure phenol of comparative example 1 of the device has a weight hourly space velocity WHSV of 10. After the reactor, the phenol was cooled to 70°C and treated continuously at 70°C on a new fixed bed ion exchange resin CT151 from Purolite with a weight hourly space velocity WHSV of 2. The final concentration of hydroxyacetone was <1 wppm and the final concentration of methylbenzofuran was <10 wppm. Compared with Comparative Example 2, the same index of methylbenzofuran concentration <10 wppm was obtained with a volume less than half of the total reaction volume.

Embodiment 3

[0069] Similar to Example 2, firstly, the impure phenol of Comparative Example 1 was continuously treated at 120° C. on fixed-bed ion exchange resin CT151 purchased from Purolite. The activity is only 20% of the new ion exchange resin. The weight hourly space velocity WHSV is 2. The phenol was then cooled to 70°C and treated continuously at 70°C on a fresh fixed bed ion exchange resin with a weight hourly space velocity WHSV of 2. The final concentration of hydroxyacetone was <1 wppm and the final concentration of methylbenzofuran was 10 wppm. Compared with Comparative Example 2, only 70% of the total reaction volume is used to obtain the same index of methylbenzofuran concentration <10 wppm. Furthermore, again compared to Comparative Example 2, half of the total reactor volume was filled with low activity resin having an activity of only 20% of the new resin, so the ion exchange resin had a longer lifetime and thus was more economical.

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Abstract

The present invention relates to a continuous method for treating a crude phenol stream comprising methylbenzofuran and hydroxyacetone by passing the crude phenol stream through at least two reactors connected in series the reactors containing an acidic ion exchange resin, whereby the temperature in successive reactors decreases in flow direction of the phenol stream so that the temperature in the first reactor in flow direction of the phenol stream is between 100°C and 200°C and the temperature in the last reactor in flow direction of the phenol stream is between 50°C and 90°C without a thermal separation step between any of two successive reactors and to the use of this method in a process for making phenol.

Description

[0001] This invention relates to a process for treating phenol, and more particularly to a continuous process for the removal of hydroxyacetone and methylbenzofuran from crude phenol streams. Background of the invention [0002] The preparation of phenols from cumene is well known. In this method, cumene is first oxidized to cumene hydroperoxide by air oxygen. This method step is often referred to as oxidation. In a second reaction step, the so-called cleavage, cumene hydroperoxide is cleaved into phenol and acetone using a strong mineral acid such as sulfuric acid as catalyst. The product from this second reaction step, the so-called cleavage product, is subsequently fractionated by distillation. [0003] Purity requirements for commercially available phenols are becoming increasingly stringent. Therefore, to operate a phenol production plant economically, the overall yield and the selectivity to the desired end product must be increased, and any of the above-mentioned im...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C37/82C07C39/04
CPCC07C37/82C07C39/04
Inventor G·洛默M·韦伯O·施努尔
Owner INEOS PHENOL & GMBH CO
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