Regeneration method for isodewaxing catalyst

A technology of isomerization dewaxing and catalyst, which is applied in the direction of catalyst regeneration/reactivation, molecular sieve catalysts, chemical instruments and methods, etc., and can solve the problems of unsuitable precious metal/molecular sieve lubricating oil isomerization dewaxing catalysts, etc.

Active Publication Date: 2018-04-03
PETROCHINA CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0008] In short, in addition to the external oxidation regeneration method, the internal reduction regeneration method disclosed in th

Method used

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  • Regeneration method for isodewaxing catalyst
  • Regeneration method for isodewaxing catalyst
  • Regeneration method for isodewaxing catalyst

Examples

Experimental program
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Effect test

Embodiment 1

[0037] (1) Cleaning oil cleaning: select highly refined low pour point minus second line distillate oil with physical and chemical properties as shown in Table 1 as solvent carrier oil, that is, low pour point minus second line after hydrofining-isomerization dewaxing-supplementary refining Distillate oil, choose decahydronaphthalene as solvent. When the catalyst is online and the reaction temperature is 365°C, the system pressure is 12.0MPa, and the liquid hourly volume space velocity is 0.85h- 1 And hydrogen oil volume ratio 500Nm 3 / m 3 Under certain reaction conditions, the raw material oil is directly switched to solvent-carrying oil, the system pressure is reduced to 10.0MPa at a rate of 1.0MPa / h, and the hydrogen-oil volume ratio is adjusted to 1500Nm 3 / m 3 , and then mix decahydronaphthalene into the carrier oil according to the proportion of 10%, and maintain the state for 72h.

[0038] (2) Nitrogen purging: reduce the temperature of the catalyst bed to 280°C at ...

Embodiment 2

[0046] (1) Cleaning oil cleaning: the diesel distillate oil produced by the hydrocracking unit with physical and chemical properties as shown in Table 1 was selected as the solvent carrier oil, and tetrahydronaphthalene was selected as the solvent. When the catalyst is online and the reaction temperature is 365°C, the system pressure is 12.0MPa, and the liquid hourly volume space velocity is 0.85h- 1 And hydrogen oil volume ratio 500Nm 3 / m 3 Under the reaction process conditions, the raw material oil is directly switched to solvent carrying oil, the temperature is naturally lowered to 340°C, and the liquid hourly volume space velocity is adjusted to 2.0h- 1 , and then decahydronaphthalene is mixed into the solvent carrying oil according to the proportion of 20%, and the state is maintained for 24h.

[0047] (2) Nitrogen purging: reduce the temperature of the catalyst bed to 280°C at a rate of 10°C / h, stop feeding the cleaning oil, then reduce the system pressure to 1.6MPa a...

Embodiment 3

[0055] (1) Cleaning oil cleaning: select the kerosene distillate oil produced by the hydrocracking unit with physical and chemical properties as shown in Table 1 as the solvent carrier oil, and select tetrahydronaphthalene as the solvent. When the catalyst is online and the reaction temperature is 365°C, the system pressure is 8.0MPa, and the liquid hourly volume space velocity is 0.85h- 1 And hydrogen oil volume ratio 560Nm 3 / m 3 Under the reaction process conditions, first reduce the system pressure to 6.0MPa at a speed of 1.0MPa / h, then switch the raw oil to solvent-carrying oil, and adjust the liquid hourly volume space velocity to 1.0h- 1 , then raise the temperature of the catalyst bed to 380°C at a rate of 10°C / h, and adjust the hydrogen-oil ratio to 750Nm 3 / m 3 , the liquid hourly volume space velocity remains unchanged, and then decahydronaphthalene is mixed into the solvent carrying oil according to the proportion of 15%, and the state is maintained for 36 hours...

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Abstract

The invention relates to a regeneration method for an isodewaxing catalyst. The isodewaxing catalyst is a precious metal/molecular sieve catalyst. The regeneration method is characterized by comprising the following steps: placing a deactivated catalyst into a reactor; and successively subjecting the deactivated catalyst to washing with cleaning oil, purging with inert gas, hydroconversion and hydrogenolysis, oxygen oxidation and hydrogen reduction so as to restore the activity of the catalyst. Different from conventional out-of-reactor regeneration methods, the method provided by the invention removes toxic matters and impurities on the surface and in the pore channels of the catalyst in the reactor through physical processes like on-line solvent cleaning and purging with inert gas such as nitrogen and chemical processeslike hydroconversion, hydrogenolysis and low-temperature oxidation without dismounting of the catalyst, so the method avoids dismounting and filling of catalyst duringout-of-reactor regeneration, degradation of noble metals due to high-temperature oxidation during out-of-reactor regeneration and deposition of sulfate converted from sulfur species on the surface ofthe catalyst during high-temperature oxidation of the sulfur species, and can effectively extend the service life of the catalyst.

Description

technical field [0001] The present invention relates to a regeneration method of isomerization dewaxing catalyst, in particular to a method for regenerating the catalyst in the reactor without dismantling the catalyst from the reactor so as to remove harmful substances deposited on the catalyst A method for regenerating an isomerization dewaxing catalyst for recovering catalyst activity. Background technique [0002] A solid hydrogenation catalyst consists of a carrier and metals. The carrier includes alumina, amorphous silicon aluminum, molecular sieve, etc., and the metals are classified into non-noble metals such as Ni, Mo, W, or noble metals such as Pt, Pd. The deactivation of hydrogenation catalysts can be divided into the following five situations: (1) poisoning, that is, impurities contained in the catalyst during preparation or impurities present in the reactants are adsorbed on the active sites of the catalyst; (2) metal sintering, the reaction temperature is extre...

Claims

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Application Information

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IPC IPC(8): B01J38/10B01J38/14B01J38/58B01J29/90
CPCB01J29/90B01J38/10B01J38/14B01J38/58
Inventor 胡胜刘彦峰高善彬田志坚阎立军迟克彬马怀军孟祥斌谭明伟李梦晨
Owner PETROCHINA CO LTD
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