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Hydrogenation catalyst for sulfur-containing liquefied gas at low temperature, and preparation method and application thereof

A hydrogenation catalyst and catalyst technology, applied in metal/metal oxide/metal hydroxide catalysts, physical/chemical process catalysts, chemical instruments and methods, etc., can solve the problems of high hydrogenation temperature, long time, and tediousness , to achieve the effect of low hydrogenation reaction temperature

Active Publication Date: 2012-10-24
CHINA PETROLEUM & CHEM CORP
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The main purpose is to provide a low-cost, high-cost solution for existing catalysts or catalyst presulfidation treatment with high temperature, long time, or high hydrogenation temperature, or complex and cumbersome preparation process, or the use of noble metal palladium as an active component and high cost. Catalyst with relatively simple manufacturing process and high low-temperature hydrogenation activity and its application method, used for low-temperature hydrogenation saturation of sulfur-containing liquefied gas

Method used

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  • Hydrogenation catalyst for sulfur-containing liquefied gas at low temperature, and preparation method and application thereof
  • Hydrogenation catalyst for sulfur-containing liquefied gas at low temperature, and preparation method and application thereof
  • Hydrogenation catalyst for sulfur-containing liquefied gas at low temperature, and preparation method and application thereof

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Experimental program
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Effect test

preparation example Construction

[0039] Catalyst preparation: Weigh a certain amount of molded Y-alumina carrier, use soluble salt of nickel, soluble salt of cobalt, soluble salt of molybdenum to make a load solution equal to the volume of the carrier, and soak the carrier in the carrier at room temperature After a certain period of time in the loading solution, the remaining soaking solution is poured out, and after drying and roasting, the required catalyst is obtained. Contain Mo 2 o 3 8.0%~20.0%, NiO 6.0%~20.0%, CoO 1~3%, the prepared catalyst is Φ3×3~5mm strip type, or clover type, specific surface area 140~200m 2 / g.

[0040] Catalyst evaluation conditions: feed temperature 35~40℃, reaction temperature 40~100℃, reaction pressure 1.5~3.0MPa, volume liquid hourly space velocity 1.5~15.0h -1 , hydrogen / olefin molar ratio 1.1~1.4.

Embodiment 1

[0042] Take by weighing a certain amount of shaped Y-alumina carrier, according to the content Mo on the final catalyst 2 o 3 Content 12.0%, NiO content 10.0%, CoO content 1.0% Quantitatively weigh ammonium molybdate tetrahydrate, nickel nitrate hexahydrate, cobalt acetate tetrahydrate, make a solution equal to the volume of the carrier, and put the Y-alumina carrier at room temperature Soak in the solution for 12 hours, pour out the remaining soaking liquid. After drying at 125°C, it was divided into three parts and fired at 350, 375°C, 400°C, and 450°C for 6 hours. The prepared catalysts are 1#, 2#, 3#, 4#, and the specific surface area is 145.2m 2 / g, 159.8m 2 / g, 176.2m 2 / g, 198.5m 2 / g.

[0043] The prepared 1#, 2#, 3# catalysts were evaluated, the feed temperature was 35°C, and the reaction temperature was 40-65°C. The evaluation results are shown in Table 1.

[0044] Table 1 Hydrogenation performance of catalysts prepared at different calcination temperatures

...

Embodiment 2

[0049] Take a certain amount of shaped Y-alumina carrier, weigh nickel nitrate hexahydrate and cobalt acetate tetrahydrate according to the final catalyst with NiO content of 20.0% and CoO content of 3.0%, and make a solution with the same volume as the carrier. Soak the carrier in the solution for 12 hours, pour out the remaining soaking solution, and dry it at 120°C; 2 o 3 Content 20.0% Weigh ammonium molybdate tetrahydrate and make a solution with the same volume as the carrier. Soak the carrier loaded with nickel / cobalt in the solution for 12 hours at room temperature, pour out the remaining soaking solution, and dry at 120°C , 350 ℃ roasting 6h. The prepared catalyst is 5# with a specific surface area of ​​151.6m 2 / g.

[0050] The 5# catalyst was evaluated, the feed temperature was 35°C, and the reaction temperature was 40-65°C. The evaluation results are shown in Table 2.

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Abstract

The invention relates to a hydrogenation catalyst for a sulfur-containing liquefied gas at low temperature, and a preparation method and an application thereof. The catalyst, using Y-Al2O3 as a carrier, has active components such as molybdenum, nickel and cobalt, and comprises, by mass percent, Mo2O 38.0 to 20.0 %, NiO 6.0 to 20.0 %, CoO 1.0 to 3.0 % and the balance being the carrier Y-Al2O3, with the specific surface area of the carrier being 140 to 200 m2 / g. The catalyst is used for hydrogenation saturation of the sulfur-containing liquefied gas at a low temperature, with a charging temperature being 35 to 40 DEG C, a reaction temperature being 40 to 100 DEG C, a reaction pressure being 2.0 to 2.5 MPa, a bulk liquid hourly space velocity being 1.5 to 15.0 h<-1>, mole ratio of hydrogen to alkene being 1.1 to 1.4, and alkene content being less that 1 % after hydrogenation. A cycle operation mode is employed which comprises steps of catalyst reduction, sulfur-containing liquefied gas hydrogenation, catalyst re-reduction, and sulfur-containing liquefied gas re-hydrogenation.

Description

technical field [0001] The invention relates to a catalyst for low-temperature hydrogenation of sulfur-containing liquefied gas and its preparation method and application, especially the preparation and application method of a catalyst for low-temperature hydrogenation of sulfur-containing liquefied gas such as coking liquefied gas. Background technique [0002] Atmospheric and vacuum, catalytic cracking, and delayed coking units in refineries by-produce a large amount of liquefied gas, which is used by most domestic enterprises as industrial or civil fuel, and the utilization rate of chemical industry is not high. [0003] Ethylene is the basic raw material of petrochemical industry. At present, domestic ethylene production capacity is increasing rapidly. In ethylene production, raw material costs account for 60-80% of production costs. Ethylene production is mainly based on steam cracking of hydrocarbons, and the cracking raw materials mainly include ethane, liquefied pet...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): B01J23/883C10G70/02
Inventor 李明玉李军马颖涛闫雨张丽梅
Owner CHINA PETROLEUM & CHEM CORP
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