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Heavy aromatic oil processing method

A processing method and technology for heavy aromatics, applied in the petrochemical field, can solve problems affecting BTX yield and catalyst service life, and achieve the effects of avoiding solvent raw material consumption, reducing raw material cost, and increasing pore volume and specific surface area

Active Publication Date: 2022-05-06
NINGBO ZHONGJIN PETROCHEM CO LTD
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  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

The particle size of this macroporous nano-beta molecular sieve is about 50-100nm, and the particle size is a bit too large. It may cause two or more aromatics to reach the acid center through the pores at the same time due to too large pores, causing polymerization to form coke and affecting BTX production. rate and service life of the catalyst
[0004] At present, the above-mentioned technical route is mostly used for the production of triphenyl products for heavy aromatics (Liu Yi et al., "Analysis of Lightweight Technology and Prospects for Heavy Aromatics", "Technology Application and Research", 2017.06, P40-P41). Method Distillation / extraction / hydrogenation combined technical route has not been reported yet

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preparation example Construction

[0062] The preparation method of described hydrorefining catalyst comprises the following steps:

[0063] 1) Drying and pulverizing the natural sponge to obtain natural sponge powder; wherein, the blast drying temperature is 40-55°C, the blast drying time is 10-24h; the blast wind speed is 3-5 m / s; obtained after crushing The particle size of natural sponge powder is 1000-2000 mesh.

[0064] 2) Mix aluminum hydroxide dry rubber powder and natural sponge powder evenly at room temperature, add extrusion aid, extrude into strips, and then perform drying and roasting treatment; wherein, the drying temperature is 100-160°C; the roasting temperature is 400- 650° C., and the calcination time is 1 to 15 hours to obtain the carrier.

[0065] 3) Adding a nonionic surfactant to the aqueous precursor solution of the metal oxide to form an impregnating solution, the precursor being a water-soluble compound corresponding to the metal element; impregnating the carrier obtained in step 2) in...

Embodiment 1

[0071] First, 5.6g of natural sponge is blast-dried, the blower wind speed is 4 m / s, the drying temperature is 45°C, and the blast drying time is 17h, and then pulverized to obtain a natural sponge powder with a particle size of 2000 mesh; the natural sponge powder is dried at room temperature Mix well with 200g aluminum hydroxide dry rubber powder (dry basis is 80%). During the mixing process, add extrusion aids, such as citric acid, in an amount that satisfies the carrier molding; after mixing evenly, the mixture is dried and roasted Get the carrier. Wherein the drying temperature is 160°C, and the drying time is 5 hours; the calcination temperature is 400°C, and the calcination time is 8 hours.

[0072]To the prepared tungsten-cobalt impregnation solution, the concentration is 32.0g metal (calculated as oxide, tungsten / cobalt ratio 3:1) / 100mL solution, 100ml in total, add lauryl alcohol polyether, the amount added is based on the total mass of the carrier Add 2% to 10% of ...

Embodiment 2

[0074] First, 5.0g of natural sponge is blast-dried, the blast speed is 5 m / s, the drying temperature is 50°C, and the blast drying time is 24 hours, and then the natural sponge powder with a particle size of 1000 meshes is obtained by crushing; the natural sponge powder is dried at room temperature Mix well with 200g aluminum hydroxide dry rubber powder (60% on a dry basis). During the mixing process, add extrusion aids, such as citric acid, in an amount that meets the needs of the carrier; after mixing evenly, the mixture is dried and roasted Get the carrier. The drying temperature is 100° C., and the drying time is 7 hours; the calcination temperature is 650° C., and the calcination time is 1 hour.

[0075] To the molybdenum-cobalt impregnation solution prepared above, the concentration is 30.0g metal (calculated as oxide, molybdenum / cobalt ratio 3:1) / 100mL solution is 100ml in total, add lauryl alcohol polyether, the addition amount is based on the total mass of the carrie...

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Abstract

The invention relates to the field of petrifaction, and discloses a heavy aromatic oil processing method which comprises the following steps: distilling heavy aromatic oil into a light fraction and a heavy fraction, extracting the heavy fraction, part of BTX tribenzene and light toluene fraction to obtain an aromatic-poor component and an aromatic-rich component, distilling the aromatic-rich component to separate the light toluene fraction and the heavy toluene fraction, and distilling the heavy toluene fraction to obtain the heavy aromatic oil. The heavy toluene fraction and the light fraction are subjected to hydrofining together, a hydrogenation product and a lean aromatic component are subjected to a further hydrocracking reaction together in a hydrocracking reactor, and a cracking product is distilled to obtain C1-C4, BTX, tribenzene, a small amount of diesel oil products and unconverted oil. According to the method disclosed by the invention, the low-cost and inferior heavy aromatic oil can be converted into liquefied gas, triphenyl and diesel oil products with high added values, and the yield of the triphenyl and the comprehensive economy of a reforming device are obviously improved.

Description

technical field [0001] The invention relates to the petrochemical field, in particular to a method for processing heavy aromatic oil. Background technique [0002] Heavy aromatic oil mainly comes from catalytic reforming and ethylene cracking units. Reform C 9 + Heavy aromatics account for about 15% to 20% of the processing capacity of reforming units. The domestic reforming processing capacity has exceeded 100 million tons per year. Reforming C 9 + The production capacity of heavy aromatics is 15-20 million tons / year. cleavage C 9 + Heavy aromatics account for 10% to 20% of the production capacity of ethylene units. Domestic ethylene cracking units have a production capacity of more than 20 million tons per year. Cracking C 9 + The production capacity of heavy aromatics is 1-2 million tons / year. In the future, with the construction of aromatics complexes and large-scale ethylene plants in my country and the expansion and transformation of existing plants, the by-pr...

Claims

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Application Information

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IPC IPC(8): C10G67/14
CPCC10G67/14C10G2300/4006C10G2300/4012C10G2300/4018C10G2300/70C10G2400/26C10G2400/30C10G2400/04Y02P20/52
Inventor 李水荣徐保岳楼巧琳
Owner NINGBO ZHONGJIN PETROCHEM CO LTD
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