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Method for producing aromatic hydrocarbon solvent oil by ethylene cracking C9 aromatic hydrocarbon fraction hydrogenation

A technology for ethylene cracking and aromatic hydrocarbons, which is applied in the treatment of hydrocarbon oil, hydrotreating process, hydrocarbon oil treatment products, etc., and can solve the problems of complex process flow, high operating cost, and many equipments

Active Publication Date: 2020-07-07
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

This is currently the main process for producing aromatic solvent oil from pyrolysis gasoline. Due to the use of the two-stage method and the gas phase circulation hydrogenation process, and in order to reduce the temperature rise of the reaction bed, both stages require a large amount of circulating oil to take away the heat of reaction. Therefore, the process is complicated, the equipment is many, and the operating cost is high.

Method used

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  • Method for producing aromatic hydrocarbon solvent oil by ethylene cracking C9 aromatic hydrocarbon fraction hydrogenation
  • Method for producing aromatic hydrocarbon solvent oil by ethylene cracking C9 aromatic hydrocarbon fraction hydrogenation
  • Method for producing aromatic hydrocarbon solvent oil by ethylene cracking C9 aromatic hydrocarbon fraction hydrogenation

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Embodiment approach

[0030] Such as figure 1 Shown, the ethylene cracking C of the present invention 9 The process flow of distillate liquid phase hydrogenation process is: ethylene cracking C 9 Fraction 1 is mixed with circulating oil 7, and after being fully dissolved with hydrogen 2, it enters the first-stage hydrofinishing reaction zone 3, and contacts with the noble metal hydrofinishing catalyst. Under relatively mild process conditions, selective hydrotreating is easy to coke Diolefins, styrene and their derivatives. Ethylene Cracking for Diene Removal 9 The aromatic fraction is fully dissolved with hydrogen again and enters the second-stage hydrofinishing reaction zone 4, where it reacts with hydrogenation protection catalyst, hydrofinishing catalyst A, hydrofining catalyst B and hydrofining catalyst successively, and saturates monoolefins under suitable conditions , and remove sulfur, nitrogen impurities and colloids, the reaction effluent enters the separator 5 for gas-liquid separatio...

Embodiment 1

[0041] Prepare solid sodium aluminate to a concentration of 200gAl 2 o 3 / L concentrated sodium aluminate solution, diluted to a concentration of 40 gAl 2 o 3 / L sodium aluminate working solution 20L (a), take and dilute to a concentration of 50gTiO 2 / L titanium sulfate working solution 2L (b). Take a 30L steel plastic tank, open the container valves of (a) and (b) at the same time, and ventilate and introduce CO with a concentration of 40v% at the same time 2 Gas, set the flow rate of (a) and (b) so that the reaction time is 50 minutes, and quickly adjust the CO 2 flow rate, keep the pH value of the system at about 10, and the reaction temperature is 35°C. 2 CO 3 The reaction mother liquor, by adjusting Na 2 CO 3 Solution flow, keep the pH value at 9.5, the reaction time is 0.5 hours, stop feeding CO 2 , and then the air was stabilized for 40 minutes, and the slurry was filtered and washed with 60°C deionized water until neutral. Microwave drying at 120°C for 20 mi...

Embodiment 2

[0043] Use 1000g of aluminum hydroxide powder, add 20mL of nitric acid, 700mL of deionized water, 450g of silica sol and additives, mix and roll, extrude into a clover shape, dry at 110°C for 3 hours, and roast at 550°C for 3 hours to obtain the carrier; Mix 21g of nickel, 75g of molybdenum oxide, 7g of cobalt carbonate, 20g of phosphoric acid and 130mL of deionized water, and dissolve at 95°C for 3 hours to obtain 200mL of Mo-Ni-Co-P co-immersion solution. Impregnated at room temperature, dried at 120°C for 3 hours, and calcined at 500°C for 3 hours to obtain Hydrofining Catalyst A. The physical properties of hydrofining catalyst A are shown in Table 2.

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Abstract

The invention discloses a method for producing aromatic hydrocarbon solvent oil by ethylene cracking C9 aromatic hydrocarbon fraction liquid-phase cyclic hydrogenation. The method includes mixing theethylene cracking C9 fraction with circulating oil, fully dissolving with hydrogen, feeding into a first hydrofining reaction zone, and carrying out contact reaction with a noble metal hydrofining catalyst; fully dissolving the diene-removed ethylene cracking C9 aromatic hydrocarbon fraction with hydrogen again to enter a second hydrofining reaction zone to be subjected to a hydrofining reactionwith a hydrogenation protection catalyst, a hydrofining catalyst A and a hydrofining catalyst B in sequence, and separating a hydrofining product to obtain the high aromatic hydrocarbon solvent oil. According to the method disclosed by the invention, the high-efficiency utilization of the ethylene cracking C9 aromatic hydrocarbon fraction is realized, and the high-aromatic hydrocarbon solvent oilwith high quality and good stability can be obtained. The invention has the characteristics of low energy consumption and long stable operation period of the device.

Description

technical field [0001] The present invention relates to a C 9 A method for producing aromatic hydrocarbon solvent oil by hydrogenation of aromatic fractions, specifically a method of cracking C with ethylene 9 The aromatic hydrocarbon distillate is used as a raw material, and the aromatic hydrocarbon solvent oil is produced by a liquid-phase circulating hydrogenation process. Background technique [0002] Ethylene cracking C 9 The aromatic fraction is separated from ethylene cracking naphtha by extraction and C 5 Fraction, C 6 ~C 8 The remaining fraction after fractionation accounts for about 10% to 15% of the total ethylene production. With the rapid development of my country's petrochemical industry, especially the improvement of ethylene production capacity, ethylene cracking C 9 The number is also increasing and will exceed 10×10 in 2010 6 t / a. At present, most ethylene plants in my country use light diesel oil and naphtha as raw materials. 9 The yield is calcul...

Claims

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Application Information

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IPC IPC(8): C10G67/14
CPCC10G67/14C10G2300/4006C10G2300/4012C10G2300/70C10G2400/18C10G2400/30
Inventor 赵威全辉姚春雷张志银孙国权刘林东
Owner CHINA PETROLEUM & CHEM CORP
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