CS241949B1 - Non-aromatic technical petrol and method of its production - Google Patents

Abstract

Sprouting is a new kind of non-aromatic of technical gasoline containing \ t cyclans and alkanes, and the process for its production sulfur-containing petroleum naphtha Lefins and aromatic hydrocarbons.

Description

The present invention relates to a non-aromatic technical gasoline containing predominantly cyclanes and alkanes and to a process for its preparation from petroleum gas contaminated with sulfur, olefins and aromatic hydrocarbons.

Concern for the environment and human health has recently been influenced by hygiene requirements for product quality in various sectors. This makes it difficult to prepare traditional materials from available raw materials in addition to the technical requirements for production and quality.

In a number of industries, technical products such as petrol such as cleaning fluids, solvents, txpod developers are used. They are mixtures of hydrocarbons boiling in the range of between 30 and 250 ° C, in particular between 130 and 210 ° C, and according to the raw material, contain aromatic, alkane and cyclanic hydrocarbons with a minimum amount of unsaturated hydrocarbon types. They are prepared by hydrotreatment and are usually de-aromatized by solvent extraction, such as diethylene glycol, to meet hygiene requirements. or sulfuric acid. Hydrogenation processes are also known which are more efficient and depend on the catalysts used and the operating conditions. The aromatic hydrogenation is strongly exothermic and at typical aromatic concentrations of about 10% -30% by weight. there is a danger of catalysts coking by sudden uncontrolled temperature increase in the catalyst bed.

The invention describes a non-aromatic technical gasoline characterized by a distillation range of 120 to 220 ° C, preferably 135 to 140 ° C, with a flash point above 21 ° C, preferably above 30 ° C, consisting of 15 to 60% by weight. of cyclanic hydrocarbons predominantly of methylcyclanic homologues with carbon numbers of 0γ to>

% 241 949 preferably Οθ to C ₁₀ , and 2 85 to 40 wt. % of alkane hydrocarbons Ογ to C ^ g, preferably Οθ to C ^ q »having a maximum aromatic hydrocarbon content, predominantly mononuclear but not benzene, up to 2% w / w; and practically free of sulfur, nitrogen and olefinic compounds. The process is based on a petroleum fraction of 30 to 220 ° C, preferably 100 to 190 ° C. The petroleum fraction is heated with 200 to 1500 vol. Hydrogen gas under a pressure of 1 to 7 MPa in three reaction sections to a temperature of 320 to 360 ° C, then 280 to 350 ° C, and last to 260 to 340 ° C in the presence of a catalyst containing 0. 2 to 0.4 wt. Pt and 0.2 to 0.4 wt. Re on alumina activated 0.1 to 1.0 wt. % of titanium dioxide and 0.5 to 2 wt. chlorine with a volumetric rate of 0.5 to 2.0 v / v The product from the third section is fed to a fractionation column of 10 to 40 TP and separated into a fraction to 120 to 145 ° C and the remainder, non-aromatic petroleum.

From the analysis of the composition of the product according to the invention and from the production process, the relationship between the new product and the production process can be assessed. From the composition, one should note the ratio between the two types of cyclic compounds, methylclopentane and cyclohexane This improves the dissolution efficiency for some applications and also affects the hygienic properties. The same applies to the remaining aromatics, which lack the lowest mononuclear homologues, especially benzene, and polyaromatics, which in turn causes the production process and the catalyst used. In the production process, the new process is based on a descending temperature regime in a three-stage reaction system. This mode successfully solves the reaction heat distribution, preventing overheating of animals. in section 1. When the temperature rise in section 1 is 385-490 ° C, the hydrogenation reaction and dehydrogenation of the naphthenes will cease to take up excess heat and stop the temperature rise to the area of increased coking. Also, the separation of the product into two components modifies the properties of the residue as a non-aromatic naphtha with a limited flash point. The lead obtained during production can be used very well, for example, in thermal fission to unsaturated gaseous hydrocarbons,

241 949 wherein the composition guarantees a high yield of propylene.

The present example describes a new solvent suitable for a variety of demanding applications and a process for its preparation according to the invention.

Example

Heavy benzine having a boiling point of 100 DEG C. containing 10% by weight of crude alkane oil was prepared. aromatics (0.5% bicyclic types), 25% wt. % cyclanic hydrocarbons (2: 3 ratio of methylcyclopentanes to cyclohexanes) and 65 wt. alkanes. The gasoline contained about 300 ppm sulfur and 0.3 wt. of olefins (Br. number - 0.6 g Br / 100 g). Gasoline was introduced into the hydrotreating stage of the reforming unit, where it was desulfurized to below 1 ppm and in the rain, the column was dewatered to below 1 ppm. It was then introduced successively into three reactors in which a catalyst containing 0.30 wt. Pt, 0.30 wt. Re on gamma alumina with 0.15 wt. % TiOg and 0.7 wt. chlorine. The catalyst was split 1: 2: 4. Petrol was fed at a rate of 0.9 v / v cat.h and 1000 v / v gas per v / v was added at 3.5 MPa.

In the reaction zones, the reaction temperatures were set according to Tab. 1 and said dearomatization of the product was achieved. It can be seen that the temperature increase in the reactors is not great and the reaction proceeded without fluctuations.

The product was distilled on a 30 TP column to give a residue, the quality of which is shown in Tab. 2 compared to technical petrol obtained from the same raw material otherwise obtained. The remainder, non-aromatic technical gasoline, was suitable for use in special cleaning fluids used also in confined spaces, resp. as a developing fluid for wet electrophoretic copying. Storage stability due to low olefin contents was also an advantage.

Table 1

241 949

Dearomatization of gasoline 100 <180 ° C in a three-reactor system.

Reactor No. 1 rel. amount of catalyst part 1 inlet temperature ° C 360 outlet temperature ° C 385 aromatics content% wt. 4,5

Br. index; mg Br / 100 g 160

345

355

1,8

320

325

0.8

Table 2

Comparison of new product with used types.

petrol no.

composition characteristics% wt.

% aromatics total bicyclic cyclans wt. Total methylcyclopentane

Br. index mg Br / 100 g real energy production costs

AND according to invention (B) lacquered C necykla nicky 0.8 17.0 0.5 0 0.8 0.1 35 28 8 20 May 14 4 30 150 800 1.3 1 2.8

F

Claims (2)

object of the invention 241 949 A non-aromatic petroleum gas having a distillation range of 120 to 220 ° C, preferably 135 to 190 ° C, a flash point above 21 ° C, preferably above 30 ° C, and consisting of 15 to 60% by weight. cyclanic hydrocarbons, predominantly methylcyclo pentane homologues with carbon numbers Ογ to C ₁₂ , preferably From 85 to 40 wt. alkane hydrocarbons C? % to C-J2, preferably ϋθ to C-jq, having a maximum aromatic hydrocarbon content, predominantly mononuclear but not benzene, up to 2 wt. and practically free of sulfur, nitrogen and olefinic compounds. A process for producing a non-aromatic technical gasoline from a hydrotreated petroleum fraction boiling between 30 to 220 ° C, preferably 100 to 190 ° C, characterized in that the petroleum fraction is heated with 200 to 1500 vol% hydrogen gas under a pressure of 1 to 7 M 3? in three reaction sections to a temperature of 320 to 360 ° C successively, then 280 to 350 ° C, and last to 260 to 340 ° C in the presence of a catalyst containing 0.2 to 0.4 wt. Pt and 0.2 to 0.4 wt. Re on alumina activated 0.1 <1.0 wt. % of titanium dioxide and 0.5 to 2 wt. chlorine with a volumetric rate of 0.5 to 2.0 v / v The product from the third reaction section is fed to a fractionation column of 10 to 40 TP and separated into fractions up to 120 to 145 ° C and the remainder, non-aromatic petroleum.