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INVENTION
Russian Federation Patent RU2258732
METHOD ennobling catalytic cracking gasoline
Name of the inventor: Gulyaev LA (RU); Khavkin VA (RU); Kaminsky EF (RU); Bychkova DM (RU); Loshchenkov IN (RU); Falkevich GS (RU); Barilchuk Mikhail (LT); Osipov LN (RU); Krasil'nikova LA
The name of the patentee: Open Joint Stock Company "All-Russian Research Institute for Oil Refining" (JSC "VNII NP")
Address for correspondence: 111116, Moscow, ul. Aviamotor, 6, JSC "VNII NP", the head of
Starting date of the patent: 2004.04.29
Usage: Refining. Essence: conduct a catalytic cracking gasoline hydrotreating. Hydrotreated product is separated into a light [NC - 110 (150) ° C] and severe [110 (150) ° C - KK] factions; heavy fraction of [110 (150) ° C - QC] is partitioned into two streams, one of which is recycled to the hydrotreating step, mixing with the feedstock, and the second is compounded with the light hydrotreated gasoline fraction [NC - 110 (150) ° C] and output installation of the system as a gasoline component (sulfur content 0,04-0,1 wt.%). The method provides a catalytic cracking gasoline to total sulfur content of less than 0.10 wt.%, Including the absence of mercaptan sulfur, with a minimum reduction of the octane number of gasoline refined from baseline catalytic cracking gasoline.
DESCRIPTION OF THE INVENTION
The invention relates to the field of oil refining, specifically to a method for refining a catalytic cracking gasoline.
Known refining method of catalytic cracking gasoline by selective hydrotreating it under a pressure of 3.1 MPa, a temperature of 200-350 ° C, feed space velocity of 3-10 h -1. As a result, the sulfur content in the hydrorefining fraction reduced from 0.15-0.30% to 0,02-0,14 wt.%, And octane number decreases by 1.5 points IM (Research method).
When selecting the optimal mode selective hydrotreating possible to ensure a reduction in average sulfur content of 0.1 wt.% (Ie. By 50-70%), while reducing the octane number by 0.5-1.5 points. Gidrogenizat obtained can be used directly as a commodity gasoline (octane 91-93 IM) or as a component of commercial gasoline (Khavkin VA, Gulyaev, LA et al. Chemistry and Technology of Fuels and Oils 2001 , №1, p.10).
The disadvantages of the method is the inability to deepen over 70% desulfurization without a sharp reduction of octane, and the need for hydrotreating and across wide gasoline fraction, which involves unreasonably high utilization of raw materials of the reaction volume, and hence increases the heat consumption of electricity, steam, water and others.
The closest to the claimed invention is a method of producing gasoline by hydrodesulfurization of the gasoline fraction of catalytic cracking in the presence of sulphide-oxide catalyst at elevated temperature and pressure of hydrogen-containing gas. Hydrodesulfurization subjected to severe unstable gasoline fraction [120 (140) ° C - QC] then return it after hydrodesulphurisation to step fractionation where it is blended with the light gasoline fraction of catalytic cracking [NC - 120 (140) ° C] and after further stabilization output with installation.
Gasoline contains 0.1-0.15% by weight obtained in this way. sulfur and is characterized by the same octane rating as the original broad gasoline fraction of catalytic cracking - about 79-80 MM - (Motor method) (RF patent №2134287, Cl C 10 G 55/06, 1999.).
A disadvantage of the method is the inability to reduce the sulfur content of gasoline in the product less than 0.10 wt%, which does not allow to obtain gasoline with a sulfur content that meets modern requirements (in accordance with GOST 51105-97 of the Russian Federation -. Not more than 0.05% by weight in Europe. - not more than 0.015% by weight -. to EN 228 standards on emissions by road to Euro-3).
Another disadvantage of this method is the inability to control the quality of light gasoline fractions [NC - 120 (140) ° C], which in some cases contains an increased amount of mercaptan - the most corrosive sulfur compounds, and their removal from the commercial gasoline and is an important task in the production process of the modern level quality.
The object of the invention to provide a process for catalytic cracking upgrading gasoline, which will reduce the sulfur content therein to a level less than 0.10 wt.%, And completely remove mercaptan sulfur from refined gasoline, which will allow the product to involve trade low sulfur gasoline. Both problems must be solved with a minimum reduction of the octane number of gasoline refined from baseline catalytic cracking gasoline (no more than 0.5-1.0 paragraph).
To solve this problem the method of catalytic cracking gasoline refining comprising hydrotreating it in the presence of a catalyst at elevated temperature and pressure and hydrogen-containing gas by compounding the title product fractions. The method is characterized in that the hydrotreated product is separated into a light [NC - 110 (150) ° C] and a heavy [110 (150) ° C - QC] fractions; heavy fraction of [110 (150) ° C - QC] is partitioned into two streams, one of which is recycled to the hydrotreating step, mixing with the feedstock, and the second is compounded with the light hydrotreated gasoline fraction [NC - 110 (150) ° C] and output installation of the system as a low-sulfur gasoline component (sulfur content 0,04-0,1 wt.%).
Wherein the ratio between the flow of the heavy gasoline fraction [110 (150) ° C - QC] returned to the hydrotreating stage, and the flow is mixed with the light hydrotreated gasoline fraction [NC - 110 (150) ° C], is from 70 to 30-70 -30% vol.
The hydrotreatment was carried out at a pressure of 2.0-4.5 MPa and a temperature of 220-360 ° C, the volumetric hourly space velocity of 2-10 h -1, a ratio of hydrogen gas / feed from 50: 1 to 300: 1 v / v.. in the presence of aluminum-cobalt-molybdenum or nickel-aluminum-molybdenum catalyst.
Moreover, the original catalytic cracking gasoline fraction withdrawn from the cracker may have different boiling range from 30 to 230 ° C (broad fraction).
The invention is illustrated by the following examples.
example 1
Catalytic cracking gasoline fraction having a boiling range 30-230 ° C, with a total sulfur content of 0.3 wt.%, Including 0.027 Mercaptan sulfur wt.%, And 89 octane (IM) is subjected to hydrorefining in the presence of alumino -kobalt-molybdenum catalyst at a temperature of 220 ° C, a pressure of 4.5 MPa, feed space velocity of 2.0 hr -1 and a ratio of hydrogen gas / feed 300:. 1 v / v. Gidrogenizat obtained by the distillation column separated into two fractions: a light - NK-110 ° C and heavy - 110 ° C and CC. The light fraction has a sulfur content of 0.037 wt%. and octane number 93 (IM). The heavy fraction is partitioned into two streams, one of which (30 vol.%) Is returned to the hydrotreating stage by mixing with the feedstock, and the second (70 vol.%) With a sulfur content of 0.017 wt%. octane and 83 (IM) is compounded with the light hydrotreated gasoline fraction NK-110 ° C and withdrawn from the installation as a component of commercial gasoline, which is characterized by a total sulfur content of 0.1 wt.%, including the absence of mercaptan sulfur and an octane rating of 88 points (IM).
example 2
Catalytic cracking gasoline fraction boiling range 70-210 ° C, the total sulfur content of 0.25 wt.%, Including 0.022% mercaptan sulfur by weight. octane and 89 (IM) is subjected to hydrorefining in the presence of aluminum-nickel-molybdenum catalyst at a temperature of 360 ° C, a pressure of 2.0 MPa, feed WHSV 10 hr -1 and a ratio of hydrogen gas / feed 50: 1 v ./about. Gidrogenizat obtained by the distillation column separated into two fractions: a light - NK-110 ° C and heavy - 110 ° C and CC. The light fraction has a sulfur content of 0.028 wt%. and octane number 92 (IM). The heavy fraction is partitioned into two streams, one of which (70 vol.%) Is returned to the hydrotreating stage by mixing with the feedstock, and the second (30 vol.%) With a sulfur content of 0.11% by weight. octane and 82 (IM) is compounded with the light hydrotreated gasoline fraction NK-110 ° C and withdrawn from the installation as a component of commercial gasoline, which is characterized by a total sulfur content of 0.049 wt.%, including the absence of mercaptan sulfur and the octane number of 88.5 points (IM).
example 3
Catalytic cracking gasoline fraction boiling range 30-230 ° C, the total sulfur content of 0.3 wt.%, Including 0.027 Mercaptan sulfur wt.%, And 89 octane (IM) is subjected to hydrorefining in the presence of aluminum-cobalt -molibdenovogo catalyst at a temperature of 300 ° C, a pressure of 3.0 MPa, feed space velocity of 5.0 hr -1 and a ratio of hydrogen gas / feed 200:. 1 v / v. Gidrogenizat obtained by the distillation column separated into two fractions: a light - NK-150 ° C and heavy - 150 ° C and CC. The light fraction has a sulfur content of 0.04% by weight. and octane number 91 (IM). The heavy fraction is partitioned into two streams, one of which (50 vol.%) Is returned to the hydrotreating stage by mixing with the feedstock, and the second (50 vol.%) With a sulfur content of 0.167 wt%. octane and 82 (IM) is compounded with the light hydrotreated gasoline fraction NK-150 ° C and withdrawn from the installation as a component of commercial gasoline, which is characterized by a total sulfur content of 0.077 wt.%, including the absence of mercaptan sulfur and octane number 88.7 points (IM).
From these examples it follows that the proposed method allows to obtain a catalytic cracking gasoline having a sulfur content less than 0.10 wt.%, Including the absence of mercaptan sulfur, with a minimum reduction of the octane number of gasoline refined from baseline catalytic cracking gasoline.
CLAIM
1. A process for upgrading FCC gasoline comprising hydrotreating it in the presence of a catalyst at elevated temperature and pressure and hydrogen-containing gas by compounding the title product fractions, wherein the hydrotreated product is separated into a light [NK-110 (150) ° C] and a heavy [ 110 (150) ° C - QC] fractions; heavy fraction of [110 (150) ° C - QC] is partitioned into two streams, one of which is recycled to the hydrotreating step, mixing with the feedstock, and the second is compounded with the light hydrotreated gasoline fraction [NC - 110 (150) ° C] and output the installation of the system as a component of commercial gasoline.
2. A method according to claim 1, characterized in that the ratio between the flow of the heavy gasoline fraction [110 (150) ° C - QC] returned to the hydrotreating stage, and the flow is mixed with the light hydrotreated gasoline fraction [NC - 110 (150) ° C], is from 30-70 vol.% to about 70 -30.%.
3. The method of claim 1 or 2, wherein the hydrotreatment is carried out at a pressure of 2.0-4.5 MPa and a temperature of 220-360 ° C, feed space velocity of 2-10 h -1, a ratio of hydrogen gas / feed from 50: 1 to 300:. 1 v / v. in the presence of aluminum-cobalt-molybdenum or nickel-aluminum-molybdenum catalyst.
print version
Publication date 07.04.2007gg
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