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Method for extracting methylnaphthalene in C10 aromatics

A technology for carbon ten aromatic hydrocarbons and methyl naphthalene is applied in the field of extracting methyl naphthalene from carbon ten aromatic hydrocarbons, which can solve the problems of low methyl naphthalene purity and yield, large equipment investment and high production cost, and achieves short cycle time and energy consumption. Low, high relative yield effect

Inactive Publication Date: 2016-01-27
SINOPEC YANGZI PETROCHEM +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Obviously, the traditional process requires 3 to 4 rectification towers to obtain fractions with different boiling points. The investment in equipment is large, the energy consumption is large, the yield is low, and the production cost is correspondingly high. and lower yield

Method used

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  • Method for extracting methylnaphthalene in C10 aromatics
  • Method for extracting methylnaphthalene in C10 aromatics
  • Method for extracting methylnaphthalene in C10 aromatics

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0031] The process of extracting methyl naphthalene from carbon deca aromatic hydrocarbons by the integrated method of continuous lateral distillation and drum crystallization, refer to figure 1 , figure 2 :

[0032] (1) The continuous intermediate feeding method is adopted, and the raw materials are pumped from the carbon deca aromatic hydrocarbon storage tank into the sideline rectification tower kettle, and heating starts when the liquid level reaches 1 / 3;

[0033] (2) When the temperature at the top and bottom of the tower becomes stable and the device reaches full reflux, the temperature at the top D-1 is 203.5-206.1℃, the temperature at the side line D-2 is 221.5-223.6℃, ​​and the temperature at the side line D-3 is 244.7~246.5℃, the temperature of tower reactor D-4 is 252.5~256.6℃;

[0034] (3) After separation, the top component is light carbon ten component, the side line D-2 component is mesitylene and naphthalene enriched liquid; the side line D-3 component is methyl naph...

Embodiment 2

[0043] The process of extracting methyl naphthalene from carbon deca aromatic hydrocarbons by the integrated method of continuous lateral distillation and drum crystallization, refer to figure 1 , figure 2 . The inlet and outlet flow rate, feeding position, reflux ratio and crystallizer temperature of the side-line rectification tower are shown in Table 3. Other conditions are the same as in Example 1, and the experimental results are shown in Table 4.

[0044] Table 3 Continuous sideline distillation and drum crystallization process conditions

[0045]

[0046] Table 4 Results of extraction of methyl naphthalene from carbon deca aromatics by continuous lateral distillation and drum crystallization

[0047]

Embodiment 3

[0049] The process of extracting methyl naphthalene from carbon deca aromatic hydrocarbons by the integrated method of continuous lateral distillation and drum crystallization, refer to figure 1 , figure 2 . The feed and discharge flow rate, feed position, reflux ratio and crystallizer temperature of the sideline rectification tower are shown in Table 5. Other conditions are the same as in Example 1, and the experimental results are shown in Table 6.

[0050] Table 5 Continuous sideline distillation and drum crystallization process conditions

[0051]

[0052] Table 6 Results of extraction of methyl naphthalene from carbon deca aromatics by continuous lateral distillation and drum crystallization

[0053]

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Abstract

The invention discloses a method for extracting methylnaphthalene in C10 aromatics. The concrete process comprises charging the raw material C10 aromatics by employing a continuous intermediate charging manner, and starting to heat when the liquid level reaches the 1 / 3 position; controlling the tower top D-1 temperature to be 203.5-206.1 DEG C, the side-stream D-2 temperature to be 221.5-223.6 DEG C, the side-stream D-3 temperature to be 244.7-246.5 DEG C, and the tower kettle D-4 temperature to be 252.5-256.6 DEG C; after separation, obtaining light C10 compositions at the tower top, obtaining a durene and naphthalene enriched solution at the side-stream D-2, obtaining a methylnaphthalene enriched solution at the side-stream D-3, and obtaining heavy C10 compositions at the tower kettle D-4; and condensing and crystallizing the side-stream D-3 composition, so as to obtain methylnaphthalene. The method is short in period, simple in operation, low in energy consumption and high in relative yield. Under the conditions that the continuous side-stream rectifying tower temperature, the charging / discharging rate and the reflux ratio are determinate, the methylnaphthalene content in the methylnaphthalene enriched solution can be improved to 88 wt% or more at one time, the yield reaches 86% or more, and after continuous crystallization, the methylnaphthalene crystal purity is 96% or more, and the yield is 86% or more.

Description

Technical field [0001] The invention relates to a method for extracting methyl naphthalene in carbon deca aromatic hydrocarbons. Background technique [0002] Carbon ten aromatic hydrocarbons refer to C by-produced in the processing of petroleum and coal 9 , C 10 , C 11 And C 11 The main sources of the above aromatic hydrocarbon mixtures are the following five types: by-product C of the catalytic reformer unit of the refinery 10 , C 11 Heavy aromatics; by-product C of wide-cut catalytic reforming unit of polyester raw material plant 10 Heavy aromatics; by-product C of ethylene plant 10 , C 11 Heavy aromatics; ethylene tar by-product of ethylene plant; heavy aromatics-coal tar by-product of coal high-temperature coking. C referred to in the present invention 10 Aromatics refers to the separation of C after extraction 5 , C 6 ~C 9 The remaining fractions after the fractions are mainly composed of naphthalene, mesitylene, methyl naphthalene and C 11 Aromatics, which contains a small ...

Claims

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Application Information

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IPC IPC(8): C07C15/24C07C7/04C07C7/14
Inventor 顾正桂汪洋陈韶辉詹其伟顾美娟姚小利蒋力
Owner SINOPEC YANGZI PETROCHEM
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