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A kind of selective hydrogenation method of gasoline

A selective and pyrolysis gasoline technology, which is applied in the field of gasoline hydrogenation, can solve the problem that diolefins do not have hydrogenation selectivity, etc., and achieve good hydrogenation activity, high hydrogenation selectivity, hydrogenation stability and thermal stability strong effect

Active Publication Date: 2015-12-02
PETROCHINA CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The catalyst can be used for hydrofining of middle and low distillate oils. It can hydrogenate saturated monoolefins to the greatest extent while hydrodesulfurizing. It can meet the requirements of oil products with variable sulfur content and high space velocity, but it has no effect on diolefins. Hydrogenation selectivity

Method used

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  • A kind of selective hydrogenation method of gasoline
  • A kind of selective hydrogenation method of gasoline
  • A kind of selective hydrogenation method of gasoline

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0043] Dissolve 20.7g of citric acid in water at 30°C, add 10.4g of lithium carbonate to prepare 60ml of aqueous solution, spray 300g of pseudo-boehmite alumina powder with this solution, knead while spraying, then add 80ml of water, 5ml of nitric acid ( 60% content) and 9.7g silica sol (containing 40% silica), continue to knead and extrude, dry at 120°C for 4 hours in the air, and roast at 980°C for 4 hours to obtain modified Al 2 o 3 carrier.

[0044] At 30°C, 86.4g of nickel nitrate, 7.2g of sodium stannate, 17.1g of zinc nitrate, 14.3g of copper nitrate, and 3.3g of ammonium molybdate were made into 90ml of aqueous solution, then 6.5g of tetraethylene glycol was added, and then immersed in 100g On the modified carrier, aging for 6 hours, drying in air at 120°C for 2 hours, and calcining at 350°C for 4 hours to prepare catalyst C-1.

Embodiment 2

[0053] Dissolve 42.6g of citric acid in water at 35°C, add 18.7g of lithium carbonate to prepare 60ml of aqueous solution, spray 300g of pseudo-boehmite alumina powder with this solution, knead while spraying, then add 80ml of water, 5ml of nitric acid ( Content 60%) and 9.7g phosphoric acid (content 85%), continue to knead and extrude, dry at 130°C for 2 hours in the air, and roast at 1050°C for 4 hours to obtain modified Al 2 o 3 carrier.

[0054] At 30°C, 80.7g of nickel nitrate, 6.6g of sodium stannate, 9.8g of zinc nitrate, 4.9g of ammonium molybdate, and 4.5g of ammonium tungstate were made into 90ml of aqueous solution, then 10.0g of triethylene glycol was added, and then immersed in 100g of the modified carrier was aged for 6 hours, dried in air at 120°C for 3 hours, and calcined at 500°C for 6 hours to obtain catalyst C-2.

Embodiment 3

[0063] Dissolve 3.0g of citric acid and 1.3g of oxalic acid in water at 40°C, add 5.3g of potassium carbonate to prepare a 60ml aqueous solution, spray 300g of pseudo-boehmite alumina powder with this solution, knead while spraying, and then add 80ml of water and 5ml of nitric acid (content 60%) and 24.9g silica sol (containing 40% silica), continue to knead and extrude into strips, dry at 120°C for 3h in the air, and roast at 1100°C for 4h to obtain modified Al 2 o 3 carrier.

[0064] At 40°C, 79.4g of nickel nitrate, 5.7g of sodium stannate, 5.6g of zinc nitrate, 3.9g of copper nitrate, 1.5g of ammonium molybdate, and 1.4g of ammonium tungstate were prepared into 90ml of aqueous solution, and then 6.9g of triethylene glycol was added , and then impregnated on 100 g of the modified carrier, aged for 6 hours, dried in air at 120° C. for 3 hours, and calcined at 550° C. for 3 hours to obtain catalyst C-3.

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Abstract

The invention relates to a selective hydrogenation method of pyrolysis gasoline. A fixed bed reactor and a nickel-base hydrogenation catalyst are adopted. The method is characterized in that the hydrogenation process conditions are as follows: liquid hourly space velocity is 1.0 to 4.0h<-1>, the inlet temperature of the reactor is 30 to 130 DEG C, the reaction pressure is more than or equal to 2.4MPa, and the hydrogen-oil volume ratio is 100-500: 1. The catalyst adopts aluminum oxide as a carrier and comprises the following components by weight percent, based on the weight of the catalyst being 100%: 14 to 19 percent of nickel oxide, 2 to 5 percent of tin oxide, 0.1 to 8 percent of alkali metal lithium oxide and / or potassium oxide, 0.5 to 8 percent of copper oxide and / or zinc oxide, 0.3 to 8 percent of molybdenum oxide and / or tungsten oxide and 0 to 8 percent of silicon dioxide and / or phosphorus oxide. The process is suitable for the selective hydrogenation of diolefin in the pyrolysis gasoline, and the hydrogenated product can be used as an excellent gasoline blending component or a raw material for producing aromatic hydrocarbon through further hydrogenation.

Description

technical field [0001] The invention relates to a gasoline hydrogenation method, which is suitable for one-stage selective hydrogenation process of pyrolysis gasoline, especially for the hydrogenation process of selective hydrogenation of diolefins into monoolefins in the one-stage hydrogenation reaction of full-fraction pyrolysis gasoline . Background technique [0002] Pyrolysis gasoline fraction is an important by-product of the ethylene industry, accounting for 50% to 80% of ethylene production. Because it is rich in aromatics and high-octane olefins, it can be used as an important source of aromatics extraction after two-stage hydrogenation. Excellent gasoline blending components can also be obtained after only one stage of hydrogenation. The first stage of hydrogenation reaction is carried out at low temperature. Pd-based or Ni-based catalysts are generally used. The purpose is to remove easily polymerizable components such as conjugated dienes and styrene, but to pre...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10G49/04B01J27/19
Inventor 马好文孙利民梁顺琴康宏敏王廷海吴杰向永生王宗宝郑云弟颉伟吕龙刚胡晓丽巩红光蒋彩兰
Owner PETROCHINA CO LTD