CS241670B1

CS241670B1 - Fuel for jet aircraft engines and its manufacturing process

Info

Publication number: CS241670B1
Application number: CS844466A
Authority: CS
Inventors: Oldrich Svajgl
Original assignee: Oldrich Svajgl
Priority date: 1984-06-15
Filing date: 1984-06-15
Publication date: 1986-04-17
Also published as: CS446684A1

Abstract

Řešení popisuje vysokojakostní letecké tryskové palivo, skládající se ze dvou složek: středně vroucí petrolejové frakce definované rozmezím bodu varu a bodem krystalizace a dearomatizované lehčí ropné frakce. Řešení dále podává postup výroby tohoto paliva z alkalické sírné ropy kombinací rektifikace, hydrorafinace a dearomatizace lehké složky. Podmínky dearomatizace a katalyzátor pro tento účel jsou zvlášt podrobně vytknuty a je zdůrazněn několikastupňový systém a platino-rheniový katalyzátor s nízkým obsahem obou kovů.The solution describes a high-quality aviation jet fuel consisting of two components: a medium-boiling kerosene fraction defined by the boiling point range and the crystallization point and a dearomatized lighter oil fraction. The solution further provides a process for producing this fuel from alkaline sulfur crude oil by a combination of rectification, hydrotreating and dearomatization of the light component. The conditions of dearomatization and the catalyst for this purpose are particularly detailed, and a multi-stage system and a platinum-rhenium catalyst with a low content of both metals are emphasized.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a high-grade jet aircraft engine fuel derived from a sulfur alkane oil consisting of a medium boiling kerosene fraction and a dearomatized light kerosene fraction and a process for producing such a fuel from said type of petroleum.

Jet aircraft fuels are characterized practically equally throughout the world by a number of parameters that affect their production from oil. The main parameters are combustion characteristics, volatility and viscosity in addition to low temperature properties. Combustion characteristics shall be defined on the one hand by the aromatic content directly and indirectly by the height of the non-flaming flame and the luminescent number. Volatility is given by the distillation curve and flash point. Fuel flow is characterized by viscosity and crystallization temperature. All parameters can be partially influenced by the type of oil. It is very difficult to produce from alkane petroleum, where a low distillation range must be chosen for the isolation of the appropriate fraction in order to obtain suitable combustion properties. The fuel viscosity is then at the border. Also, the yield of a fraction suitable as jet fuel from such petroleum is very limited and interferes with the range of gasoline boiling points. This reduces the amount of gasoline from petroleum, both for reforming and for the production of gaseous olefins by thermal cracking.

The invention defines a high-quality jet aircraft engine derived from a sulfur alkane oil as a mixture of 40 to 85% by volume hydrotreated petroleum fraction I boiling in the range of 140 to 150 ° C, preferably 180 to 235 ° C, with a crystallization point of -45 to -55 And 15 to 60% by volume of the dearomatized petroleum fraction II boiling in the range of 120 to 220 ° C, preferably 135 to 185 ° C. The invention further provides a process for producing such high quality jet aircraft fuel from an alkane sulfur oil by a combination of distillation rectification, hydrotreating, and hydrotreating dearomatization. The process is such that a petroleum fraction A boiling between 20 and 180 ° C and a petroleum fraction B boiling preferably between 180 and 235 degrees Celsius are separated from the crude oil by distillation. In parallel, both fractions are freed from 90 to 99.9% sulfur compounds on standard hydrotreatment catalysts, such as cobalt and / or nickel-molybdenum, at pressures of 4 to 4 MPa, at elevated temperatures. Fraction A is then fed to a distillation apparatus where it is freed from portions up to 80-100 ° C and then the residue above 80-100 ° C is fed to a multi-stage dearomatization system at temperatures of 200-380 ° C, under a pressure of 2-4 MPa. at a flow rate of 0.5 to 2 v / v % catalyst per hour in the presence of a hydrogen-containing gas and a catalyst containing 0.2 to 0.4 wt. Pt and Re on pure alumina and then on distillation, where the distillate is separated to 135 ° C and fraction II, which is mixed with hydrotreated fraction B, referred to above as fraction I.

From the above-mentioned fuel composition and method of manufacture, fundamental changes can be seen from the prior art given by the new invention. It can be seen that the two fractions I and II suitably follow each other and the indicated crystallization point limits the yield of fraction I and its distillation range. The production process involves, as a major part, the dearomatization of one component, a component which can be desulfurized under normal conditions to very low residual sulfur concentrations. The multi-stage dearomatization system is preferably commonly used in gasoline reforming. Also the catalyst for this reaction is a novel, usually not used for hydrogenation, platinum promoted rhenium. The conditions recommended for dearomatization include implicitly possible temperature regimes of the multistage process, descending and / or ascending with different advantages and disadvantages in terms of the level of dearomatization and energy intensity. Dearomatization of the heavy naphtha has considerable advantages over dearomatization of the kerosene fraction, which is considerably more difficult to desulfurize to S values below 1 ppm.

In particular, the descending dearomatization mode has priority in a system of several reaction layers. The first layer is kept at a temperature of 20 to 40 ° C below the limit temperature at which the hydrogenation changes to dehydrogenation. This ensures that part of the aromatics is removed without causing an excessive temperature rise and possibly coking of the catalyst. Cooling downstream of the first reaction step then allows the next part of the dearomatization to be conducted at thermodynamically more advantageous parameters.

In the example below, details of the fuel composition as well as the method of production thereof are included. These parameters characterize the invention but are not limiting.

Example

In the Sulfur Alkane Oil Refinery, jet aviation fuel is produced by distilling the 160 to 210 ° C kerosene fraction from 6% by weight petroleum, hydrotreating the kerosene fraction and stabilizing it from HaS and lighter constituents. The fuel quality marked with number 1 is shown in Tab. 1 together with standardized requirements. It can be seen that the fuel is relatively low-boiling, has at its limits viscosity and combustion properties, i.e. the height of the non-toxic flame (VNP) and the luminescence number (LC). In production, the relative yield of gasoline is reduced by 5%, ie by 25%. This reduces the distillation section of the catalytic reforming feedstock from 180 to 160 ° C.

According to the invention, fuel No. 2, which is also listed in Tab. 1. The required quantity of gasoline up to 180 ° C, ie 20 wt. and 9 wt. kerosene fractions boiling between 180 and 235 ° C. The kerosene fraction was characterized by a crystallization point of 241670 ce which should not be higher than -50 ° C. Next to the hydrogenation refining in parallel with gasoline up to 180 ° C. The hydrotreatment was carried out on a cobalt-molybdenum catalyst for a kerosene fraction and a cobalt-molybdenum catalyst on a petrol. The hydrotreated gasoline was then fed to a three-stage dearomatization unit, where it was hydrogenated under a pressure of 3.5 MPa and at a rate of volume] of Table 2. The products of the distillation of the dearomatized gasoline are also listed.

Gradual mixing of the residue above 135 ° C, whose yield from the hydrogenated product was 50%, with the hydrotreated kerosene fraction gave fuel No. 2, included for comparison in Table 1. The differences in the most important properties are underlined. Fuel

size 1,0 vol / vol of the catalyst. with a hydrogen to hydrocarbon ratio of 1,200: 1 by volume. The temperature in the first section was maintained at 360 degrees Celsius, the second at 340 ° C and the third at 325 degrees Celsius. The feedstock and the hydrogenation product in the presence of Pt-Re catalyst (0.3 wt% Pt and 0.3 wt% Re per alum) Table 1 Comparison of conventional jet fuel and fuel according to the invention has a higher viscosity, better

Claims

SUBJECT

1. Aircraft jet propellant fuel derived from sulfuric alkane oil, characterized in that it consists of 40 to 85% by volume of hydrotreated petroleum fraction I boiling in the range of 140 to 250 ° C, preferably 180 to 235 ° C, with a point of crystallization from -45 to -55 ° C and from 15 to 60% by volume, dearomatized petroleum fraction II boiling in the range of 120 to 220 ° C, preferably 135 to 185 ° C.

2. A process for producing high-quality jet aircraft fuel from an alkane-sulfur oil by a combination of distillation rectification, hydrotreating and hydrogenation dearomatization, characterized in that the petroleum fraction A boiling between 20 and 180 [deg.] C and the kerosene fraction B boiling preferably between 180 and 235 ° C,

BACKGROUND OF THE INVENTION both fractions are simultaneously freed from sulfur compounds of 90 to 99.9% on standard hydrotreating catalysts, such as cobalt and / or nickel molybdenum, at pressures of 2 to 4 MPa, at elevated temperatures and fraction A is then led to distillation to remove up to 80-100 ° C, and then the residue above 80-100 ° C is fed to a multi-stage dearomatization system, at temperatures of 200-380 ° C, under a pressure of 2-4 MPa, at a volumetric rate of 0.5-2 vol / vol. . % catalyst per hour in the presence of a hydrogen-containing gas and a catalyst containing 0.2 to 0.4 percent by wt. Pt and Re on pure alumina and then on distillation, where the distillate is separated to 135 ° C and fraction II, which is mixed with fraction I, obtained by hydrotreating fraction B.

Severography, n. P., Rívod 7, Most

Price 2.40 KCe