Method for producing high-octane petrol

A technology for high-octane gasoline and heavy gasoline, applied in gasoline stabilization, petroleum industry, cracking, etc., can solve the problems of large olefin loss and low gasoline yield, increase gasoline yield and octane number, and avoid olefins The effect of excessive loss

Active Publication Date: 2009-07-01
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AI-Extracted Technical Summary

Problems solved by technology

Since the whole distillate gasoline is refined back in this method, the ...
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The invention relates to a method for producing high-octane petrol, which comprises the following steps: introducing raw oil into a catalytic cracking reactor to be contacted with a catalyst and react under the catalytic cracking reaction condition; separating the reaction oil gas and the catalyst to be generated which is reclaimed after steam stripping and regeneration; introducing the reaction oil gas into a subsequent fractionation part; and separating out heavy petrol and light diesel fuel fractions with the distillation range of between 100 and 300 DEG C by the fractionation part, and pouring the fractions with or without hydrogenation into the catalytic cracking reactor for freshening. By adopting the method, a common catalytic cracking unit and a common catalyst can be used, the prior device is unnecessary to be changed significantly, and the heavy petrol and the light diesel fuel fractions are introduced back into the catalytic cracking reactor respectively for freshening with major reactions of chain scission reaction of arene lateral chains and transalkylation reaction so as to improve the petrol yield and the octane number.

Application Domain

Catalytic crackingGasoline stabilisation

Technology Topic

TransalkylationDistillation +7


  • Method for producing high-octane petrol
  • Method for producing high-octane petrol
  • Method for producing high-octane petrol


  • Experimental program(2)
  • Comparison scheme(1)

Example Embodiment

[0036] Example 1
[0037] This example illustrates that the method provided by the present invention can increase the yield of FCC gasoline and increase the gasoline octane number.
[0038] Using the test device in the comparative example, the FCC gasoline was cut into light and heavy gasoline by distillation. Among them, the distillation range of heavy gasoline is 160-220°C. The catalytically cracked diesel is cut into light and heavy diesel by the method of distillation, and the distillation range of the light diesel is 168-281°C. The heavy gasoline and light diesel oil are mixed into a mixed oil, enter the riser reactor from below the catalytic cracking feedstock nozzle, and react with the catalyst MLC-500. The feedstock oil and reaction conditions are the same as the comparative example. The reacted oil and gas and catalyst go up to the raw material feeding reaction section, and the generated oil and gas and spent agent continue to go up into the separation system to separate the reaction product from the catalyst. After the catalyst is stripped, it is sent to the regenerator for scorching and regeneration, and the main reaction is recycled. The conditions, product distribution and properties of gasoline products are listed in Table 5.
[0039] It can be seen from Table 5 that compared with the comparative example, using the method provided by the present invention, the gasoline yield increased by 26.47%, the dry gas yield decreased by 1.55%, the oil slurry decreased by 9.09%, and the coke yield decreased by 2.11%. The content of aromatics in gasoline increased significantly by 15.52 percentage points, and the research octane number increased by 1.7 units.

Example Embodiment

[0040] Example 2
[0041] This example illustrates that the method provided by the present invention can increase the yield of FCC gasoline and increase the gasoline octane number.
[0042] The test device, feedstock oil and catalytic cracking reaction conditions used in this example are the same as those in Example 1, except that light diesel oil is firstly hydrorefined and then mixed with catalytically cracked heavy gasoline into a medium riser reactor for reaction. The conditions of hydrorefining are: reaction temperature is 350°C, pressure is 3.2MPa, hydrogen-to-oil volume ratio is 300:1, and volumetric space velocity in weight hour is 2.5h -1. The properties of the mixed oil are shown in Table 4. Product distribution and properties are shown in Table 5.
[0043] It can be seen from Table 5 that compared with Example 1, the gasoline yield of the mixed oil after hydrogenation is increased by 1.18% after refining, but the aromatics content in gasoline is 10.67% lower than that in Example 1. The octane number of the research method is better than that of the implementation. Example 1 is slightly lower, but 0.6 units higher than the comparative example.
[0044] Table 1
[0045] raw material Density (20℃), g/cm 3 0.9053 Viscosity (100℃), mm 2 /s 13.60 Residual carbon, weight% 2.3 Distillation range, ℃ Initial boiling point 268 5% 370 10% 400 30% 453 50% 480 70% 521 Dry point
[0046] Table 2
[0047] catalyst MLC-500 Chemical composition, weight% Al 2 O 3 44.7 Fe 2 O 3 0.38 Physical properties Specific surface area, m 2 /g 203 Pore volume, ml/g 2.14 Apparent density, g/cm 3 0.7921 Sieve composition,% 0~40μm 8.5 0~80μm 66.3 0~110μm 87.2 0~150μm 95.9
[0048] table 3
[0049] catalyst RN-10 Chemical composition, weight% Nickel oxide 4.0 Tungsten oxide 26.0 fluorine 2.0 Physical properties: Specific surface, m 2 /g 230 Pore volume, ml/g 0.27 Crushing strength, N/mm 27.5
[0050] Table 4
[0051] Mixed oil properties Example 1 Example 2 Density, g/cm 3 0.8527 0.8475 Distillation range, ℃ Initial boiling point 165 164 50% 223 222 Final boiling point 267 266
[0052] table 5
[0053] Instance number Comparison Example 1 Example 2 Reaction conditions Temperature, ℃ 460 460 460 Pressure, MPa 0.2 0.2 0.2 Weight hourly space velocity, hour -1 13 13 13 Agent-oil ratio 9 9 9 Water vapor/raw material weight ratio 0.11 0.11 0.11 Product distribution, weight% Dry gas


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