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Method for recovering aromatic hydrocarbons in oil with low aromatic hydrocarbon content

A low-aromatic and aromatic technology, which is used in the treatment of hydrocarbon oil, hydrocarbon oil treatment products, petroleum industry, etc., can solve the problems of many new dosages, high extraction temperature, low yield, etc., and achieves moderate operating conditions and avoids solvent decomposition. , the effect of low extraction temperature

Active Publication Date: 2018-10-23
PETROCHINA CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0007] The existing aromatics extraction process is not suitable for raw oils with low aromatics content for two reasons: 1. the existing aromatics extraction process is suitable for processing raw materials with aromatics content of 30-90%, and the dearomatization efficiency for low aromatics content raw materials is low; 2. Use the existing aromatics extraction process to dearomatize the raw material oil with low aromatics content. The extraction temperature is high, the extraction agent is easy to decompose, and the yield is low. When recycling, there are many new dosages, and the overall energy consumption is high.

Method used

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  • Method for recovering aromatic hydrocarbons in oil with low aromatic hydrocarbon content

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Effect test

Embodiment 1

[0026] The aromatic content of the raw oil is 5.83%, the ratio of the raw oil entering the pre-fractionator 1 and the extraction tower 3 is 1:1, and the feed volume space velocity of the pre-fractionator is 1.5h -1 , the temperature at the bottom of the tower is 75°C, the temperature at the top of the tower is 60°C, the operating pressure is 0.15MPa; the volumetric space velocity of the extraction tower is 0.53h -1 Sulfolane is used as the extractant, the solvent ratio (solvent feed amount / extraction raw material amount) is 1.6, the operating temperature is 55°C, and the operating pressure is 0.15MPa; the stripping dose / extracted oil volume ratio is 1.6, the stripping tower operating temperature is 55°C, and the operating pressure 0.15MPa; Distillation tower bottom temperature 85°C, tower top temperature 60°C, operating pressure 0.17MPa, side line production temperature 75°C, backwashing ratio 0.6; washing water volume / mass to be washed 0.1, washing unit operating temperature 2...

Embodiment 2

[0028] The aromatics content of the raw oil is 24.66%, the ratio of the raw oil entering the pre-fractionator 1 and the extraction tower 3 is 2:1, and the feed volume space velocity of the pre-fractionator is 1.5h -1 , the temperature at the bottom of the tower is 80°C, the temperature at the top of the tower is 65°C, the operating pressure is 0.13MPa; the volumetric space velocity of the extraction tower is 0.37h -1 , Sulfolane is used as the extractant, solvent ratio (solvent feed amount / extraction raw material amount) 3.0, operating temperature 70°C, operating pressure 0.25MPa; stripping dose / extracted oil volume ratio 2.0, stripping tower operating temperature 70°C, operating pressure 0.25MPa; Distillation tower bottom temperature 90°C, tower top temperature 65°C, operating pressure 0.31MPa, side line production temperature 75°C, backwashing ratio 0.8; washing water volume / mass to be washed 0.1, washing unit operating temperature 30°C, The operating pressure is 0.12MPa; th...

Embodiment 3

[0030] The aromatic content of the raw oil is 10.16%, the ratio of the raw oil entering the pre-fractionator 1 and the extraction tower 3 is 3:1, and the feed volume space velocity of the pre-fractionator is 1.5h -1 , the temperature at the bottom of the tower is 76°C, the temperature at the top of the tower is 61°C, the operating pressure is 0.12MPa; the volumetric space velocity of the extraction tower is 0.45h -1 Sulfolane is used as the extractant, the solvent ratio (solvent feed amount / extraction raw material amount) is 2.2, the operating temperature is 65°C, and the operating pressure is 0.20MPa; the stripping dose / extracted oil volume ratio is 1.8, the stripping tower operating temperature is 65°C, and the operating pressure 0.20MPa; Distillation tower bottom temperature 86°C, tower top temperature 61°C, operating pressure 0.27MPa, side line production temperature 75°C, backwashing ratio 0.7; washing water volume / mass to be washed 0.1, washing unit operating temperature ...

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Abstract

The invention relates to a method for recovering aromatic hydrocarbons in oil with low aromatic hydrocarbon content. According to the method, raw oil is subjected to pre-fractionation, extraction, re-extraction, distillation, washing with water and water distillation so as to obtain a mixed aromatic hydrocarbon product. The method has the advantages of mild operation conditions, low comprehensiveenergy consumption and good dearomatization effect, and is applicable to recovery of aromatic hydrocarbons from a mixture with low aromatic hydrocarbon content.

Description

technical field [0001] The invention relates to a method for recovering aromatics in oil with low aromatics content used in oil refining or chemical enterprises. Background technique [0002] As the main means of industrial separation of aromatics in reformed oil and pyrolysis gasoline, aromatics extraction is divided into liquid-liquid extraction and extractive distillation according to the process principle. Liquid-liquid extraction is the separation of aromatics and non-aromatics by utilizing the different solubility of hydrocarbon components in solvents. [0003] The traditional liquid-liquid extraction process is that after the wide distillate oil is cut, it is sent into the middle of the extraction tower through a feed pump, and poor solvents such as dimethyl sulfoxide, sulfolane, N-methylpyrrolidone, N-formyl morpholine and tetraethylene glycol Added from the upper part of the extraction tower, the two phases are in countercurrent contact, the aromatics and a small a...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10G53/04
CPCC10G53/04C10G2300/4025C10G2300/4081C10G2400/30
Inventor 王艳飞唐晓东曹耀武周金波任海鸥李晶晶程中克苟文甲董炳利马艳捷施红
Owner PETROCHINA CO LTD
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