Hydrogenation catalyst and continuous production method

A hydrogenation catalyst and catalyst technology are applied in the field of distillate oil hydrogenation, which can solve the problems of low production efficiency and unstable product quality, and achieve the effects of improving production efficiency, improving surface acidity and reducing production costs.

Active Publication Date: 2018-11-13
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0005] At present, the production methods of pseudo-boehmite are mainly inorganic aluminum salt method and organic aluminum salt method. The production process mostly adopts batch tank react

Method used

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  • Hydrogenation catalyst and continuous production method
  • Hydrogenation catalyst and continuous production method
  • Hydrogenation catalyst and continuous production method

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0044] This example introduces the preparation method of Mo, Ni, ammonia original solution. In this example, only one concentration and ratio of Mo, Ni, and ammonia original solutions are prepared, and solutions of other ratios and concentrations can be prepared according to the method introduced.

[0045] Get 296g ammonium molybdate, 105g nickel nitrate is put into multi-necked flask, after adding a certain amount of deionized water, stir until the substance in the bottle is slurry, then slowly add 150g ammoniacal liquor, slowly heat after the initial reaction, Keep the solution temperature at 70-80°C for 1-2 hours, stop heating, filter the obtained solution while it is hot, and then add ammonia water to adjust the pH of the solution to 10.0-12.0 to obtain the required solution. The solution composition is MoO 3 : 58.2g / 100ml; NiO: 10.5g / 100ml.

Embodiment 2

[0047]Dimethylammonium chloride 300g, ammonium tetrafluoroborate 190g, pure water 450g, mixed, heated to 80°C under stirring, kept at constant temperature for 1h, clarified, naturally cooled to about 30°C, centrifuged to filter out the solid to obtain 300g of ionic liquid, The water content is about 3.5wt%, and the yield is 73wt%.

[0048] Add 2L of bottom water to the reaction tank and each swing tank, heat the temperature of the reaction tank to 60°C, heat each swing tank to 90°C, adjust the stirring rate of the reaction tank to 200rad / min, adjust the stirring speed of each reaction tank to 400rad / min; open the feed inlet at the upper end of the reactor, and the concentration is 100g / 100mlAl with the flow velocity of 60ml / min 2 o 3 Aluminum sulfate solution and a concentration of 100g / 100ml Al at a flow rate of 40ml / min 2 o 3 Add the sodium metaaluminate solution in the reaction tank, adjust the pH value to 8.5, and after stabilizing for 10 minutes, open the overflow port...

Embodiment 3

[0050] 400g of triethylammonium chloride, 220g of sodium hexafluorophosphate, and 450g of pure water were mixed, heated to 90°C under stirring, kept at a constant temperature for 3 hours, clarified, naturally cooled to about 30°C, and centrifuged to filter out the solid to obtain 450g of ionic liquid I. The water content is about 3.5wt%, and the yield is 72wt%.

[0051] Add 3L of bottom water to the reaction tank and each swing tank, heat the temperature of the reaction tank to 80°C, heat each swing tank to 100°C, adjust the stirring rate of the reaction tank to 300rad / min, adjust the stirring speed of each reaction tank To 500rad / min; Open the feed inlet at the upper end of the reactor, with the flow velocity of 80ml / min, the concentration is 80g / 100mlAl 2 o 3 Aluminum sulfate solution and a concentration of 100g / 100ml Al at a flow rate of 30ml / min 2 o 3 Add the sodium metaaluminate solution in the reaction tank, adjust the pH value to between 7.5, and after stabilizing fo...

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Abstract

The invention discloses a hydrogenation catalyst and a continuous production method. The hydrogenation catalyst comprises, based on the weight of the catalyst, 61-92wt% of aluminum oxide supporter, active metal and auxiliaries, wherein the active metal is selected from one or more or from group VIII and/or group VIB metal elements and comprises based on the weight of oxide, 1-9wt% and preferably 1.0-5.0wt% of group VIII metal and 5-25wt% and preferably 10-20wt% of group VIB metal, and the weight percentage of the auxiliaries is 2-5wt% based on the weight of elements. The hydrogenation catalysthas the advantages that high surface active metal and auxiliary density in the catalyst is achieved, and the concentration of the active metal gradually increases from inside to outside along particle size. The method has the advantages that high hydrogenation active metal utilization rate is achieved, the surface acidity of the catalyst can be improved effectively, the inactivation speed of thecatalyst is slowed, continuous production of the hydrogenation catalyst is achieved, production efficiency is increased, and production cost is lowered.

Description

technical field [0001] The invention relates to the field of hydrogenation of distillate oil, in particular to a hydrogenation catalyst and a continuous production method. Background technique [0002] Crude oil and distillates derived from crude oil contain impurities such as sulfur, nitrogen, oxygen and metals. The existence of these impurities not only affects the stability of the oil, but also emits SO during use. X , NO X and other harmful gases pollute the environment. During the secondary processing of oil products, the presence of impurities such as sulfur, nitrogen, oxygen and metals can poison catalysts. Therefore, removing the above-mentioned impurities is an important process in oil processing. Distillate oil hydrotreating refers to the process of contacting raw oil and hydrogen with a catalyst at a certain temperature and pressure to remove impurities and saturate aromatics. [0003] Typical hydrotreating catalysts are metal oxides of Group VIII and VIB of ...

Claims

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Application Information

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IPC IPC(8): B01J27/132B01J27/19B01J35/08B01J35/10B01J37/04C10G45/08
Inventor 吕振辉佟佳彭绍忠薛冬张学辉杨涛
Owner CHINA PETROLEUM & CHEM CORP
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