US 2026/0286235 A1Published application

Heavy oil hydrorefining method

AssigneeEneos Corporation

InventorsChikanori NAKAOKA, Masaya KANI, Koichi MATSUSHITA, Ryo KISHIDA

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Abstract

A heavy oil hydroprocessing method includes a step of sequentially bringing a heavy oil into contact with a first hydrogenation catalyst, a second hydrogenation catalyst, and a third hydrogenation catalyst, which are placed in a downflow-type fixed bed reaction apparatus, in the presence of hydrogen. Both the first hydrogenation catalyst and the second hydrogenation catalyst include macropores and mesopores. The pore distribution of the first hydrogenation catalyst has a peak at a pore diameter of 50 nm or more and a peak at a pore diameter of less than 50 nm. The pore distribution of the second hydrogenation catalyst also has a peak at a pore diameter of 50 nm or more and a peak at a pore diameter of less than 50 nm. The volume V1MACRO of the macropores in the first hydrogenation catalyst is larger than the volume V2MACRO of the macropores in the second hydrogenation catalyst.

Claims17

Dependent claims

A heavy oil hydroprocessing method, comprising sequentially bringing a heavy oil into contact with a first hydrogenation catalyst, a second hydrogenation catalyst, and a third hydrogenation catalyst in the presence of hydrogen, wherein

the first hydrogenation catalyst, the second hydrogenation catalyst, and the third hydrogenation catalyst are placed in a downflow-type fixed bed reaction apparatus,
the first hydrogenation catalyst, the second hydrogenation catalyst, and the third hydrogenation catalyst are different catalysts,
both the first hydrogenation catalyst and the second hydrogenation catalyst include macropores and mesopores,
a pore diameter of the macropores is 50 nm or more,
a pore diameter of the mesopores is less than 50 nm,
a pore distribution of the first hydrogenation catalyst has a peak where a pore volume at a pore diameter of 50 nm or more reaches a local maximum and a peak where a pore volume at a pore diameter of less than 50 nm reaches a local maximum,
a pore distribution of the second hydrogenation catalyst has a peak where a pore volume at a pore diameter of 50 nm or more reaches a local maximum and a peak where a pore volume at a pore diameter of less than 50 nm reaches a local maximum,
a volume V1MACRO of the macropores in the first hydrogenation catalyst is larger than a volume V2MACRO of the macropores in the second hydrogenation catalyst,
a specific surface area of the first hydrogenation catalyst is 185 m2/g or more,
a specific surface area of the second hydrogenation catalyst is 160 m2/g or more, and
a content of a Group 6 element in the second hydrogenation catalyst is 5 mass % or more and 7 mass % or less.

8 more elements

the first hydrogenation catalyst, the second hydrogenation catalyst, and the third hydrogenation catalyst are placed in a downflow-type fixed bed reaction apparatus,
the first hydrogenation catalyst, the second hydrogenation catalyst, and the third hydrogenation catalyst are different catalysts,
both the first hydrogenation catalyst and the second hydrogenation catalyst include macropores and mesopores,
a pore diameter of the macropores is 50 nm or more,
a pore diameter of the mesopores is less than 50 nm,
a pore distribution of the first hydrogenation catalyst has a peak where a pore volume at a pore diameter of 50 nm or more reaches a local maximum and a peak where a pore volume at a pore diameter of less than 50 nm reaches a local maximum,
a pore distribution of the second hydrogenation catalyst has a peak where a pore volume at a pore diameter of 50 nm or more reaches a local maximum and a peak where a pore volume at a pore diameter of less than 50 nm reaches a local maximum,
a median pore diameter PD1MACRO of the macropores in the first hydrogenation catalyst is a pore diameter at which a cumulative volume of the macropores in the pore distribution of the first hydrogenation catalyst reaches 50% of the total volume of the macropores,
a median pore diameter PD2MACRO of the macropores in the second hydrogenation catalyst is a pore diameter at which a cumulative volume of the macropores in the pore distribution of the second hydrogenation catalyst reaches 50% of the total volume of the macropores,
the median pore diameter PD1MACRO is larger than the median pore diameter PD2MACRO,
a specific surface area of the first hydrogenation catalyst is 185 m2/g or more,
a specific surface area of the second hydrogenation catalyst is 160 m2/g or more, and
a content of a Group 6 element in the second hydrogenation catalyst is 5 mass % or more and 7 mass % or less.

10 more elements

Dependencies are inferred from the claim text.