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Heavy aromatic oil hydrofining catalyst and heavy aromatic oil processing method

A hydrorefining and catalyst technology, applied in the petrochemical field, can solve the problems affecting the yield of BTX and the service life of the catalyst, and achieve the effects of virtuous recycling, strong water absorption, and protection of the global environment

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

AI Technical Summary

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

Method used

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  • Heavy aromatic oil hydrofining catalyst and heavy aromatic oil processing method
  • Heavy aromatic oil hydrofining catalyst and heavy aromatic oil processing method

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preparation example Construction

[0052] As preferably, the preparation method of the heavy aromatic oil hydrotreating catalyst comprises the following steps:

[0053] 1) Dry and pulverize the natural sponge to obtain natural sponge powder. Wherein, the blast drying temperature is 40-55° C., the blast drying time is 10-24 hours; the blast wind speed is 3-5 m / s; the particle size of the natural sponge powder obtained after pulverization is 1000-2000 mesh.

[0054] 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.

[0055] 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; impregna...

Embodiment 1

[0069] First, 4.0g of natural sponge is blast-dried, the blower wind speed is 3 m / s, the drying temperature is 55°C, and the blast drying time is 15h, and then pulverized to obtain a natural sponge powder with a particle size of 1000 mesh; the natural sponge powder is dried at room temperature Mix well with 220g aluminum hydroxide dry rubber powder (80% on a dry basis), add extrusion aids during the mixing process, such as citric acid, the amount used is to meet the carrier molding; after mixing evenly, the mixture is dried and roasted Get the carrier. The drying temperature is 120° C., and the drying time is 5 hours; the calcination temperature is 500° C., and the calcination time is 1 hour.

[0070]To the prepared tungsten-cobalt impregnation solution, the concentration is 25.0g 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 the a...

Embodiment 2

[0072] First, 4.8g of natural sponge is blast-dried, the blower wind speed is 5 m / s, the drying temperature is 40°C, and the blast drying time is 10h, 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 180g aluminum hydroxide dry rubber powder (dry basis is 70%). During the mixing process, add extrusion aids, such as citric acid, in an amount to meet 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 7 hours; the calcination temperature is 400°C, and the calcination time is 15 hours.

[0073] To the molybdenum-cobalt impregnation solution prepared above, the concentration is 25.0g 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 carrier Add 2% ...

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Abstract

The invention relates to the field of petrifaction, and discloses a heavy aromatic oil hydrofining catalyst and a heavy aromatic oil processing method, and the catalyst comprises a metal oxide and a carrier (prepared from natural sponge and aluminum hydroxide dry glue powder). The processing method comprises the following steps: A) distilling the heavy aromatic oil into a light fraction and a heavy fraction; b) extracting the heavy fraction and n-heptane to obtain an aromatic-poor component and an aromatic-rich component; c) distilling the aromatic-poor component to separate n-heptane, a pure aromatic-poor component and a pure aromatic-rich component; d) performing hydrofining reaction on the pure aromatic-rich component and the aromatic-rich component; e) hydrogenation products, light fractions and pure lean aromatic components are subjected to a hydrocracking reaction; f) obtaining C1-C4, BTX tribenzene and diesel oil products through distillation.The catalyst has the advantages of being large in specific surface area and good in activity, low-cost and inferior heavy aromatic oil can be converted into liquefied gas, tribenzene and diesel oil products with high additional value, and the yield of tribenzene 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 heavy aromatic oil hydrotreating catalyst and a heavy aromatic oil processing method. 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 ...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): B01J23/883B01J23/888B01J35/10C10G45/08C10G69/02
CPCB01J23/883B01J23/888B01J37/0018C10G45/08C10G69/02C10G2300/202C10G2400/30C10G2300/70B01J35/23B01J35/638B01J35/635B01J35/615Y02P20/52
Inventor 李水荣徐保岳楼巧琳
Owner NINGBO ZHONGJIN PETROCHEM CO LTD
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