Catalytic conversion method for hydrocarbon oil raw material

A catalytic conversion method and catalytic cracking technology are applied in the field of catalytic cracking process and can solve the problems of high octane number, low olefin content and high olefin content in gasoline

Active Publication Date: 2008-06-04
CHINA PETROLEUM & CHEM CORP +1
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  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0003] CN1746265A discloses a catalytic cracking processing technology. The light diesel oil fraction obtained by the process is returned to the catalytic cracking unit for re-refining, the obtained heavy diesel oil fraction is subjected to solvent extraction, and the extracted heavy aromatics are used as products, and the raffinate oil is returned to the catalytic cracking unit. Refining, but this method has the problems of low gasoline yield and high gasoline olefin content
[0004] How to use catalytic cracking cycle oil to produce gasoline products with low olefin content and high octane number is a problem that puzzles those of ordinary skill in the art, and the above-mentioned prior art does not solve this problem

Method used

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  • Catalytic conversion method for hydrocarbon oil raw material
  • Catalytic conversion method for hydrocarbon oil raw material
  • Catalytic conversion method for hydrocarbon oil raw material

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0064] Refining of light fractions of light cycle oil

[0065] Atmospheric pressure residue enters the reactor and contacts with FCC catalyst MLC-500, at 500°C, agent-to-oil ratio 8, space velocity 8 hours -1 Cracking under certain conditions, fractionation after catalytic cracking to obtain dry gas, liquefied gas, gasoline, light cycle oil, heavy cycle oil, heavy oil, wherein the light cycle oil is cut into light fractions of light cycle oil at 275°C (i.e. <275 ℃ fraction, its partial properties are shown in Table 2) and the heavy fraction of light cycle oil, and then the light fraction of part of light cycle oil (accounting for 15% by weight of the atmospheric residue) is returned to the catalytic cracking reactor and carried out together with the atmospheric residue cracking reaction. The product distribution and gasoline product properties are shown in Table 3 and Table 4, respectively.

Embodiment 2

[0071] The heavy fraction of light cycle oil is mixed with heavy cycle oil for hydrogenation.

[0072] Mix the heavy fraction of the light cycle oil obtained in Example 1 with the heavy cycle oil fraction, contact with hydrogen and hydrogenation catalyst RN-10, at a temperature of 350°C, and a liquid hourly space velocity of 1.5 hours -1 , hydrogen-to-oil ratio (that is, the volume ratio between hydrogen and hydrogenation feedstock) 350Nm 3 / m 3 , Hydrogenation under the condition of hydrogen partial pressure 2.5MPa. The properties of heavy fraction of light cycle oil and heavy cycle oil fraction before and after hydrofining are shown in Table 5.

Embodiment 3

[0074] The heavy fraction of the light cycle oil is mixed with the mixed hydrogenation product of the heavy cycle oil and the light fraction of the light cycle oil for back refining.

[0075] The light fraction of the light cycle oil obtained in Examples 1 and 2, hydrogenated diesel oil (both accounting for 10% by weight of the atmospheric residue) and the atmospheric residue are mixed into the reactor, contacted with the FCC catalyst MLC-500, and heated at 500 ° C. , agent-to-oil ratio 8, space speed 8 hours -1 Cracking under certain conditions, fractionation after catalytic cracking to obtain dry gas, liquefied gas, gasoline, light cycle oil, heavy cycle oil, and heavy oil. The product distribution and gasoline properties are shown in Table 6 and Table 7, respectively.

[0076]From Table 6 and Table 7, it can be seen that the yield of gasoline obtained from the light fraction of 10 wt% light cycle oil and 10 wt% hydrogenated diesel oil from back refining increased by 11.94 ...

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Abstract

The invention discloses a catalytic conversion method for a hydrocarbon oil raw material. The hydrocarbon oil raw material contacts the catalytic cracking catalyst in a catalytic cracking reactor, the reaction oil gas and a spent catalyst are separated, then the spent catalyst is made steam stripping and regeneration and then returns to the catalytic cracking reactor for repeated use, the reaction oil gas is fractionated to obtain dry gas, liquefied gas, gasoline, light circulating oil, heavy circulating oil and heavy oil; the light circulating oil and any diesel fraction are cut into the light fraction of the light circulating oil and the heavy fraction of the light circulating oil; the heavy fraction of the light circulating oil is mixed with the heavy circulating oil and contacts the hydrogen and the hydrorefining catalyst, the reaction effluent is separated to obtain gas, naphtha and hydrogenated diesel, the hydrogen is reclaimed and then is circularly used; the light fraction of the light circulating oil independently or the light fraction of the light circulating oil along with the hydrogenated diesel returns to the catalytic cracking reactor. The method converts the catalytic cracking circulating oil into the gasoline with low olefin content and high octane value, and improves the yield of the gasoline and the yield of the propylene.

Description

technical field [0001] The present invention belongs to a process combining a catalytic cracking process of hydrocarbon oil in the absence of hydrogen and a hydrotreating process. Background technique [0002] The world's demand for oil is increasing, and the quality of crude oil is becoming increasingly heavy and inferior. The processing of inferior raw materials by catalytic cracking units is an inevitable problem. The proportion of residual oil in the raw materials processed by the catalytic device is also increasing, the sulfur and nitrogen content of the raw materials increase, and the product quality declines. Large and low cetane number, it needs to be modified and blended with straight-run diesel to be used as commercial diesel. At present, domestic and foreign diesel oil upgrading mostly adopts hydrofining or selective aromatics extraction, but the cost of single selective hydrofining is high; selective aromatics extraction affects the yield of upgraded diesel oil,...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10G69/04
Inventor 毛安国徐先荣
Owner CHINA PETROLEUM & CHEM CORP
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