Heavy oil refining method
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experimental example 1
[0055] A heavy oil, which is a residue having an API gravity of 14.3 (a hydrogen content of 11.25 wt %; a Ni+V metal content of 65 wtppm; a Conradson carbon residue (below, abbreviated "CCR") of 11.1 wt %; and a S content of 3.95 wt %) is charged into the solvent extraction process unit as a feed oil, and using a normal pentane solvent (a solvent / oil ratio of 8 / 1), a deasphalted oil (below, abbreviated "DAO") is obtained by extraction and separation so that the extraction rate is 81 wt %, subsequently this DAO is subject to a refining process under the following hydrorefining conditions, and thereby the refined oil 1 of the present invention is obtained.
[0056] Hydrorefining conditions: Ni / Mo+Ni / Co / Mo catalyst (a specific volume ratio of 1 / 9), a hydrogen partial pressure of 90 atm; an H.sub.2 / Oil ratio of 600 Nm.sup.3 / kl; a temperature of 380.degree. C.; and an LHSV of 0.5 (1 / hr).
[0057] The yield of the obtained DAO and the refined oil with respect to the feed oil, the hydrogen conte...
experimental example 2
[0058] The feed oil used in Experimental Example 1 is charged into the solvent extraction process unit, using a normal pentane solvent (a solvent / oil ratio of 8 / 1), the DAO is obtained by extraction and separation so as to attain an extraction rate of 84 wt %, and subsequently the DAO is subject to hydrorefining under conditions identical to those of Experimental Example 1 to obtain the refined oil 2 of the present invention.
[0059] The yield of the obtained DAO and the refined oil 2 with respect to the feed oil, the hydrogen content, the amount of increase in the hydrogen content in each process, the V+Ni content, the CCR, and the sulfur content are shown in Table 1.
experimental example 3
[0060] The feed oil used in Experimental Example 1 is charged into the solvent extraction process unit, using a normal pentane solvent (a solvent / oil ratio of 8 / 1), the DAO is obtained by extraction and separation so as to attain an extraction rate of 84 wt %, and subsequently the DAO is subject to a refining process under the following hydrorefining conditions to obtain the refined oil 3 of the present invention.
[0061] Hydrorefining conditions: Ni / Mo+Ni / Co / Mo catalyst (a specific volume ratio of 1 / 9), a hydrogen partial pressure of 85 atm; an H.sub.2 / Oil ratio of 600 Nm.sup.3 / kl; a temperature of 360.degree. C.; and an LHSV of 0.5 (1 / hr).
[0062] The yield of the obtained DAO and the refined oil 3 with respect to the feed oil, the hydrogen content, the amount of increase in the hydrogen content in each process, the V+Ni content, the CCR, and the sulfur content are shown in Table 1.
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