采用环烷基减压渣油生产润滑油基础油
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摘要
采用三段高压加氢工艺(加氢处理-异构脱蜡-补充精制),以海洋环烷基减压渣油经丙烷脱沥青工艺所得的脱沥青油为原料,生产润滑油基础油。结果表明:在脱沥青油加氢处理反应压力为15 MPa,氢油体积比为1 000∶1,体积空速为0.4 h~(-1),反应温度为385或382℃;异构脱蜡反应压力为15 MPa,氢油体积比800∶1,体积空速为0.8 h~(-1),反应温度为340或345℃;补充精制反应温度为260℃的条件下,所得生成油中大于490℃馏分可达到150 BS光亮油的要求;≥280～360℃馏分可用于生产变压器油基础油;≥360～420℃馏分可用于生产橡胶增塑剂环烷基矿物油产品;≥420～490℃馏分可用于生产橡胶增塑剂环烷基矿物油产品。润滑油馏分总收率占脱沥青油的85%以上,150 BS光亮油收率约占脱沥青油的40%。
With deasphalting oil from propane deasphalting process of naphthenic vacuum residue as raw material,the lubricating base oil was produced by the three-stage high-pressure hydrogenation process(hydrotreating-isomerization dewaxing-supplementary refining).The results showed that under the conditions of reaction pressure of deasphalted oil hydrotreating15 MPa, hydrogen to oil(volume ratio)1 000∶1, space velocity 0.4 h~(-1), reaction temperature 385 or 382 ℃; the reaction pressure of isomerization dewaxing 15 MPa, hydrogen to oil 800∶1, volume of space velocity 0.8 h~(-1), the reaction temperature 340 or 345 ℃; the reaction temperature of supplementary refining 260 ℃,above 490 ℃ fraction in generation of oil could achieve 150 BS bright oil requirements ≥280-360 ℃ fraction could be used in the production of transformer base oil; the ≥360-420 ℃ fraction of plasticizer naphthenic mineral oil could be used in the production of rubber products; the ≥420-490 ℃ fraction could be used in the production of rubber plasticizer naphthenic mineral oil products. The total yield of lubricating oil fraction accounted for over 85% of deasphalted oil, and the yield of 150 BS bright oil was approximately 40% of deasphalted oil.
With deasphalting oil from propane deasphalting process of naphthenic vacuum residue as raw material,the lubricating base oil was produced by the three-stage high-pressure hydrogenation process(hydrotreating-isomerization dewaxing-supplementary refining).The results showed that under the conditions of reaction pressure of deasphalted oil hydrotreating15 MPa, hydrogen to oil(volume ratio)1 000∶1, space velocity 0.4 h~(-1), reaction temperature 385 or 382 ℃; the reaction pressure of isomerization dewaxing 15 MPa, hydrogen to oil 800∶1, volume of space velocity 0.8 h~(-1), the reaction temperature 340 or 345 ℃; the reaction temperature of supplementary refining 260 ℃,above 490 ℃ fraction in generation of oil could achieve 150 BS bright oil requirements ≥280-360 ℃ fraction could be used in the production of transformer base oil; the ≥360-420 ℃ fraction of plasticizer naphthenic mineral oil could be used in the production of rubber products; the ≥420-490 ℃ fraction could be used in the production of rubber plasticizer naphthenic mineral oil products. The total yield of lubricating oil fraction accounted for over 85% of deasphalted oil, and the yield of 150 BS bright oil was approximately 40% of deasphalted oil.
引文
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[3]赵凯,孙进发,陈晓华,等.加氢法生产石蜡基高黏度及高黏度指数润滑油基础油技术的工业应用[J].石油炼制与化工,2015,46(5):66-69.
[4]孟祥彬,高善彬,孙发民,等.石蜡基原料油加氢异构脱蜡制润滑油基础油催化剂的研制[J].石油炼制与化工,2014,45(11):33-37.
[5]孙国权,姚春雷,全辉,等.全氢法生产润滑油基础油技术的开发及工业应用[J].石油炼制与化工,2014,45(10):77-82.
[6]汪军平,许孝玲,王华,等.超高黏度指数润滑油基础油生产工艺研究[J].石油炼制与化工,2014,45(8):82-86.
[7]张翠侦,焦祖凯,徐岩峰,等.减压渣油制备150 BS 光亮油的工艺研究[J].石化技术与应用,2018,36(5):308-310.
[8]李大东,聂红,孙丽丽.加氢处理工艺与工程[M].北京:中国石化出版社,2016.