DD261604A1 - PROCESS FOR THE PRODUCTION OF BASE OILS - Google Patents

Abstract

The invention relates to a process for the hydrogenating treatment of heavy hydrocarbon fractions for the production of basic oils. The process proceeds when using a catalyst containing nickel oxide and molybdenum oxide dispersed in an Al 2 O 3 -containing carrier material. The catalyst contains a Y zeolite component whose crystals are enveloped by an outer layer of nickel and alumina.

Description

Field of application of the invention

The invention relates to a process for the hydrogenating treatment of heavy hydrocarbon fractions for the preparation of base oils, including the other conventional process stages.

Characteristic of the known technical solutions

It is known, for the production of base oils, to subject heavy hydrocarbon fractions to a hydrogenating treatment, also in combination with a solvent extraction, in which, in addition to substantially removing the hetero compounds, in particular the nitrogen compounds, by converting aromatic compounds, in particular polycyclic aromatic compounds, the required properties are significantly preformed become. Such hydrogenation processes are based on the use of special bifunctional catalysts with well-matched hydrogenation and ₍ cleavage function and the application of relatively stringent process conditions Special requirements exist for low viscosity index, high boiling, high heteroatom content starting materials Hetero compounds, and in particular an excellent selectivity for a targeted conversion of the polycyclic aromatic conditions.The expected favorable process conditions, such as low working temperature, high potential catalyst loading, limited process pressure and maximum yield determine the economy of the process, as well as the characteristics of the base oils. Catalysts which have proven useful as hydrogenating components are a metal of the VIth subgroup of the PSE, such as, for example, molybdenum and tungsten, and a metal of the VIII. Subgroup of the PSE, such. As nickel. Furthermore, the addition of Y zeolite is known. It is also common. Arrange combinations of different types of catalysts in different ways in a reactor. The catalysts are to be dried and sulfurized before commissioning in a known manner. However, the catalysts prepared and activated in this way still do not meet all the requirements with regard to the desired reaction success.

Object of the invention

It is an object of the invention to develop a process for the preparation of base oils, with the more favorable operating conditions, in particular a lowering of the working temperature, and improved characterizing properties, such. As viscosity-temperature and aging behavior, the base oils are to be achieved.

Explanation of the essence of the invention

The invention has for its object to provide a process for the preparation of base oils by hydrogenating heavy hydrocarbon fractions of the boiling range of 620 to 82O ⁰ K under high pressure conditions in the presence of a catalyst of the type Ni-Mo-Y zeolite and A ^ Oa-containing carrier material develop. It should be less than 40 vol .-% below 620 ⁰ K boiling components incurred.

According to the invention the object is achieved by a method in which the heavy hydrocarbon fractions at pressures of 10 to 30 MPa, temperatures of 650 to 700 ⁰ K, contact loads of 0.3 to 1.3V / Vh and gas product ratios of 400 to 1000 m ³ iN / m ³ and a catalyst of the type Ni-Mo-Y zeolite and AI ₂ O ₃ -containing support material are refined, the nickel oxide and molybdenum oxide distributed in an Al ₂ O ₃ -containing support material contains, and a Y-zeolite component with a module of about 40 in fine distribution, the crystals of an outer layer of nickel and aluminum oxide wrapped

According to a further feature of the invention may be ^about: h proportionately in the rear part of the reactor in combination with a catalyst according to DD-PS used 157,198th

The hydroraffinate obtained by the process according to the invention is subjected to distillation in a known manner, wherein z. B. petroleum petroleum, diesel fuel, transformer oil, spindle oil and neutral oil fractions or fuel fractions a wide Topp residue oil fraction are obtained, which nachraffiniert in a known manner partly with selective solvents, generally subjected to a solvent dewaxing and optionally by bleaching earth or be refined by hydrogenating treatment.

Surprisingly, it has been found that when the process according to the invention is carried out with comparatively low hydrogenation component contents, excellent refining performances and a special hydrogenation effect in the light lubricating oil fractions are achieved.

embodiment

1. In a reactor, about 73% of the type of catalyst usually used is replaced completely or proportionally in the rear part of the reactor by the catalyst A according to the invention. The catalyst A has the following composition: Ni 4Ma .-%

MoO ₃ 18Ma .-% Na ₂ O 0.03 Ma .-%

SiO ₂ 24.5% by mass

Al ₂ O _{3 to} 100 Ma .-%

The catalyst is sulfurized with H ₂ S-containing recycle gas at 30 MPa process pressure by heating it to about 20 ° K / h to reaction temperature.

With the thus activated catalyst, a petroleum vacuum distillate is treated by hydrogenation. Properties of petroleum vacuum dietetate

Boiling range ° K 653 to 813

Density at 323 ⁰ K g / cm ³ 0.901

Viscosity at 323 ⁰ K mm ² / s 48.4

% By weight 1.95

mg NH ₃ / I 469

19.0

Sulfur base number

% C _A (aromatically bound carbon)

ε 325 (UV-max extraction coefficient at 325 '

Conradsontest Operating conditions Catalyst quantity Pressure

Load temperature gas product ratio

K)

Wt .-%

1.7 0.11

cm ₃ 300

MPa 30

V / Vh 1.0

⁰ K 671

NI / I 1000: 1

The characteristics of the obtained raffinates and the neutral oils I obtained are shown in the table below:

In comparison, the same vacuum distillate in a reactor fully equipped with the usual type B catalyst is processed to the same raffinate density. The results are compared with those of the catalyst A in the table below.

^2/3 Catalyst B Catalyst B

Catalyst A 73 Catalyst A (comparative catalysis)

Hydrogenation temperature ⁰ K Refining density at 323 ⁰ K to 323 ⁰ K sd. Shares Base number% C _A

325

Aniline point Iodine number Vl of neutral oil I

It is necessary that catalyst A with lower working temperature causes improved degradation of condensed aromatics (ε ₃₂₅ ) and that the Vl in the light lubricating oil fractions (neutral oil I) is significantly higher.

671 677 682 0,836 0,836 0,836 24 24 24 2 3 5 9.7 8.6 8.1 0,025 0.08 0.12 93.2 93.2 93.2 2.8 3.0 3.3 94 86 79

Claims (2)

A process for the preparation of base oils for quality lubricating oils by hydrogenating treatment of heavy hydrocarbon fractions under high pressure conditions using a catalyst containing nickel oxide and molybdenum oxide in an Al ₂ O ₃ -containing carrier material, characterized in that the catalyst comprises a Y zeolite component contains a modulus of about 40 in fine distribution, the crystals of which are enveloped by an outer layer of nickel and alumina. 2. The method according to claim 1, characterized in that approximately ^1/3 of the catalyst may be proportionally included in the rear part of the reactor in combination with the catalyst according to DD-PS 157,198th