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Styrene separation process

A separation method and technology of styrene, applied in the direction of distillation purification/separation, organic chemistry, etc., can solve the problems of large loss of styrene, large loss of styrene, poor evaporation effect, etc., to reduce equipment investment, not easy to deactivate, The effect of improving the flash evaporation capacity

Inactive Publication Date: 2005-11-16
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0011] The technical problem to be solved by this invention is to overcome the polymerization loss problem of styrene in the crude styrene separation tower that is not involved in the existing literature and the problem that styrene is lost more due to the self-polymerization of styrene in the existing industrial equipment, and the problems in the previous literature It does not involve the material treatment of the purified styrene separation tower tower or the current industrial device through the film evaporator. On the one hand, the equipment investment is high and it is easy to be damaged. On the other hand, the evaporation effect is poor, and the loss of styrene is large. A new method is provided. Styrene Separation Method

Method used

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Effect test

Embodiment 1

[0019] Crude styrene raw material liquid is composed of the following mass flow components: benzene 13.86 kg / h, toluene 59.68 kg / h, non-aromatic 2.78 kg / h, ethylbenzene 1345.85 kg / h, styrene 2533.7 kg / h, p-xylene 0.35 kg / h, m-xylene 0.17 kg / h, o-xylene 0.03 kg / h, cumene 0.02 kg / h, α-methylstyrene 4.91 kg / h, heavy components 65.80 kg / h, polymer 57.49 kg / hour and water 4.17 kg / hour. The crude styrene raw material liquid enters the middle part of the crude styrene separation tower, and the crude styrene fractionation tower is a packed tower with 80 trays in total, of which 27 trays are in the rectification section. The pressure at the top of the tower is 12KPa, and the temperature at the top of the tower is 71 ℃, the pressure of the tower bottom is 21KPa, the temperature of the tower bottom is 96°C, the reflux ratio of the top reflux liquid is 7.6, the temperature of the reflux liquid is 45°C, and the mass flow rate of the top material of the crude styrene separation tower is 8....

Embodiment 2

[0022] According to the conditions and steps of Example 1, only the pressure at the top of the crude styrene separation tower was changed to 15KPa, the temperature at the top of the tower was 75°C, the pressure at the bottom of the tower was 24KPa, the temperature at the bottom of the tower was 99°C, and the reflux ratio of the top reflux liquid was 8.0 , the temperature of the reflux liquid is 50°C, the total plate number of the crude styrene separation tower is 70, and the rectification section is 22 trays; the operating temperature of the flash tank is 120°C, the operating pressure is 30KPa, and the cycle is calculated by weight ratio To the amount of tar in the middle of the flash tank: the amount of tar discharged is 140: 1. As a result, the weight percent concentration of styrene in the crude styrene separation tower overhead material is 1.63%, and the weight percent concentration of styrene in the output tar 15 It is 4.98%, and the loss of styrene polymerization is 6.1 k...

Embodiment 3

[0024] According to the conditions and steps of Example 1, only the pressure at the top of the crude styrene separation tower was changed to 10KPa, the temperature at the top of the tower was 65°C, the pressure at the bottom of the tower was 18KPa, the temperature at the bottom of the tower was 90°C, and the reflux ratio of the top reflux liquid was 7.0 , the reflux liquid temperature is 40 ℃; the operating temperature of the flash tank is 140 ℃, and the operating pressure is 15KPa, and the amount of tar in the middle part of the flash tank is circulated by weight ratio: the amount of tar discharged is 80: 1, and the result is: crude The weight percent concentration of styrene in the top material of the styrene separation tower is 0.74%, the weight percent concentration of styrene in the discharged tar 15 is 3.69%, and the styrene polymerization loss is 2.8 kg / ton of styrene product.

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Abstract

The present invention relates to a separation method of styrene, and is aimed at mainly resoving the problems of that existent separation equipment is high in investment and easy to be damaged, evaporation effect is poor and styrene loss is high. Said invention adopts a technical scheme, and its characterized by that a dehydrogenation liquor is used, and fed into crude styrene separation tower, after separation the tower top product is passed through the ethylbenzene recovery tower to make separation to obtain product flow containing toluene and benzene, and the ethylbenzene is circulated in reaction zone, then the tower bottoms of crude styrene separation tower can be fed into the fine styrene separation tower to make separation and obtain fine styrene from tower top, and the tower bottom tar material containing styrene is passed through adiabatic flash tank to make flash evaporation.

Description

technical field [0001] The invention relates to a method for separating styrene. Background technique [0002] Styrene is widely used as a raw material for the production of various resins, plastics and elastomers, and its wide range of applications is mainly due to the ease with which styrene can be polymerized (for example, to form polystyrene) or copolymerized (for example, with butadiene to form Production of rubber) adaptability. [0003] The production of styrene is well known in terms of the dehydrogenation process and the various catalysts used in the process. The main research objective at present is to improve the efficiency of this process. Especially known is the dehydrogenation process of ethylbenzene, wherein the dehydrogenation is carried out in a set comprising at least two dehydrogenation reactors in series and placed between the reactors, wherein the reaction effluent is heat exchanged with steam heated in a heating device....

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C7/04C07C15/46
Inventor 邵百祥朱冬茂谢在库毛连生
Owner CHINA PETROLEUM & CHEM CORP
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