CN111718749A - 一种废矿物油分离处理方法及系统 - Google Patents
一种废矿物油分离处理方法及系统 Download PDFInfo
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- CN111718749A CN111718749A CN202010605886.8A CN202010605886A CN111718749A CN 111718749 A CN111718749 A CN 111718749A CN 202010605886 A CN202010605886 A CN 202010605886A CN 111718749 A CN111718749 A CN 111718749A
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- mineral oil
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- 239000002699 waste material Substances 0.000 title claims abstract description 83
- 239000002480 mineral oil Substances 0.000 title claims abstract description 78
- 235000010446 mineral oil Nutrition 0.000 title claims abstract description 78
- 238000000926 separation method Methods 0.000 title claims abstract description 46
- 238000004821 distillation Methods 0.000 claims abstract description 35
- 239000000047 product Substances 0.000 claims abstract description 28
- 239000010779 crude oil Substances 0.000 claims abstract description 21
- 238000010438 heat treatment Methods 0.000 claims abstract description 21
- 238000009833 condensation Methods 0.000 claims abstract description 20
- 230000005494 condensation Effects 0.000 claims abstract description 20
- 239000002199 base oil Substances 0.000 claims abstract description 19
- 239000007787 solid Substances 0.000 claims abstract description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000007670 refining Methods 0.000 claims abstract description 15
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- 239000007789 gas Substances 0.000 claims description 13
- 238000009835 boiling Methods 0.000 claims description 12
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- 210000000214 Mouth Anatomy 0.000 claims description 8
- 239000010865 sewage Substances 0.000 claims description 7
- 239000002351 wastewater Substances 0.000 claims description 7
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N phenol Chemical compound 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OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 6
- 239000002910 solid waste Substances 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 4
- 239000012530 fluid Substances 0.000 claims description 4
- 238000003860 storage Methods 0.000 claims description 4
- HYBBIBNJHNGZAN-UHFFFAOYSA-N Furfural Chemical group 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O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 claims description 3
- 239000002737 fuel gas Substances 0.000 claims description 3
- SECXISVLQFMRJM-UHFFFAOYSA-N n-methylpyrrolidone Chemical compound 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CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 3
- 239000011780 sodium chloride Substances 0.000 claims description 3
- ZMXDDKWLCZADIW-UHFFFAOYSA-N dimethylformamide Substances 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- NINIDFKCEFEMDL-UHFFFAOYSA-N sulfur Chemical compound 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[S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000010409 thin film Substances 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G53/00—Treatment of hydrocarbon oils in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/04—Treatment of hydrocarbon oils in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
- C10M175/0025—Working-up used lubricants to recover useful products ; Cleaning by thermal processes
- C10M175/0033—Working-up used lubricants to recover useful products ; Cleaning by thermal processes using distillation processes; devices therefor
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
- C10M175/005—Working-up used lubricants to recover useful products ; Cleaning using extraction processes; apparatus therefor
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
- C10M175/0083—Lubricating greases
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
- C10M175/02—Working-up used lubricants to recover useful products ; Cleaning mineral-oil based
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M177/00—Special methods of preparation of lubricating compositions; Chemical modification by after-treatment of components or of the whole of a lubricating composition, not covered by other classes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1003—Waste materials
- C10G2300/1007—Used oils
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/10—Lubricating oil
Abstract
本发明公开了一种废矿物油分离处理方法及系统，包通过对待处理废矿物油进行预处理脱除固体，然后将预处理后的废矿物油在100℃‑200℃下进行初馏分离，去除粗油和水分，在通过将初馏分离后的废矿物油经过加热至260℃‑300℃经过多级减压蒸馏，采用多级减压蒸馏方法，能够实现废矿物油的真空切割，不需要进行分子蒸馏，简单可靠，将减压蒸馏后的气相产物换热冷凝形成液体产物，将液体产物通过溶剂萃取精制得到符合标准的润滑油基础油，即可实现废矿物油的分离可再生，提高废矿物油的重复利用率，本发明工艺简单、原料适用性广、投资和运行成本低、收率高、工艺过程安全环保。
Description
技术领域
本发明属于废矿物油再生领域，具体涉及一种废矿物油分离处理方法及 系统。
背景技术
废矿物油是因受杂质污染、氧化和热的作用，改变了原有的理化性能而 不能继续使用而被更换下来的矿物油，主要来自于石油开采和炼制产生的油 泥和油脚，车辆、机械维修和拆解过程中产生的废发动机油、制动器油、自 动变速器油、齿轮油等废润滑油。它是由多种物质组成的复杂混合物，主要 成份有C15-C36的烷烃、多环芳烃(PAHs)、烯烃、酚类等，对人体有特定的 毒性和危害性，直接排放将对生态环境造成严重的污染，已被列入《国家危 险废物名录》。
目前废矿物油的再生方法通常包括物理法和化学法两种方法，物理法即 采用絮凝、过滤、离心、沉降、蒸馏、薄膜蒸发、溶剂萃取等方法对废矿物 油进行回收；化学法则以氧化精制(如酸洗)和加氢精制为主。将上述两种 方法进行组合可以形成多种再生工艺，比如蒸馏－酸洗－白土工艺、蒸馏－ 加氢工艺、蒸馏－溶剂精制工艺、膜分离工艺等。蒸馏－酸洗－白土工艺在 生产过程中会产生大量的废酸、废水、废气和废渣，造成严重的二次污染， 并且产品质量低下，逐渐面临淘汰。蒸馏—加氢工艺不产生酸渣和酸水，环 境污染小，产品质量高，但是废油加氢精制对于工艺路线和催化剂性能提出 了更高的要求，废油中的各种杂质对于催化剂的性能和寿命影响非常大。蒸 馏—溶剂精制工艺也是一种环境友好型工艺，是国家鼓励发展的除加氢工艺 之外的另一种工艺，存在的问题主要是溶剂损耗大，基础油收率相对较低， 基础油产品硫含量高。
发明内容
本发明的目的在于提供一种废矿物油分离处理方法及系统，以克服现有 技术的不足。
为达到上述目的，本发明采用如下技术方案：
一种废矿物油分离处理方法，包括以下步骤：
步骤1)、对待处理废矿物油进行预处理脱除固体；
步骤2)、将预处理后的废矿物油在100℃-200℃下进行初馏分离，去除 粗油和水分；
步骤3)、将初馏分离后的废矿物油经过加热至260℃-300℃经过多级减 压蒸馏，将减压蒸馏后的气相产物换热冷凝形成液体产物，将液体产物通过 溶剂萃取精制得到符合标准的润滑油基础油。
进一步的，废矿物油自原料罐区通过泵送入离心机分离设备进行预处理， 将废矿物油中的固体废物脱除。
进一步的，具体的，将预处理后的废矿物油加热至100℃-200℃送入脱 水塔，废矿物油在入脱水塔的塔顶将水分和低沸点的粗油蒸出，水份经凝后 废水送污水处理，低沸点的粗油送进罐区。
进一步的，脱水塔塔顶压力为常压或者负压。
进一步的，所述溶剂采用糠醛、苯酚、N-二甲基酰胺或N-甲基吡咯烷酮。
进一步的，采用加热方式为导热油、熔盐炉或者燃料气加热炉。
一种废矿物油分离处理系统，包括油液固体分离设备、脱水塔和多级减 压塔，液固体分离设备的液体出料口与脱水塔入料口通过加热管道连通，脱 水塔的液体出料口与多级减压塔的入料口通过加热管道连通，多级减压塔的 气相出口通过冷却管道连通至储液槽，多级减压塔的塔釜产品出口连接至塔 釜产品存储罐。
进一步的，脱水塔的气相出口通过冷凝管连接至冷凝处理。
进一步的，油液固体分离设备具体采用离心机。
进一步的，多级减压塔采用三段减压塔或者为三个单减压塔依次串联。
与现有技术相比，本发明具有以下有益的技术效果：
本发明一种废矿物油分离处理方法，包通过对待处理废矿物油进行预处 理脱除固体，然后将预处理后的废矿物油在100℃-200℃下进行初馏分离， 去除粗油和水分，在通过将初馏分离后的废矿物油经过加热至260℃-300℃ 经过多级减压蒸馏，采用多级减压蒸馏方法，能够实现废矿物油的真空切割， 不需要进行分子蒸馏，简单可靠，将减压蒸馏后的气相产物换热冷凝形成液 体产物，将液体产物通过溶剂萃取精制得到符合标准的润滑油基础油，即可 实现废矿物油的分离可再生，提高废矿物油的重复利用率，本发明工艺简单、原料适用性广、投资和运行成本低、收率高、工艺过程安全环保。
进一步的，废矿物油自原料罐区通过泵送入离心机分离设备进行预处理， 方法简单，去除效率高。
进一步的，将预处理后的废矿物油加热至100℃-200℃送入脱水塔，废 矿物油在入脱水塔的塔顶将水分和低沸点的粗油蒸出，水份经凝后废水送污 水处理，低沸点的粗油送进罐区，通过预处理方法，能够提高废矿物油中水 分和低沸点的粗油的处理，提高后期多级减压蒸馏精度和效率。
一种废矿物油分离处理系统，包括油液固体分离设备、脱水塔和多级减 压塔，液固体分离设备的液体出料口与脱水塔入料口通过加热管道连通，脱 水塔的液体出料口与多级减压塔的入料口通过加热管道连通，多级减压塔的 气相出口通过冷却管道连通至储液槽，多级减压塔的塔釜产品出口连接至塔 釜产品存储罐，采用多级减压蒸馏方法，能够实现废矿物油的真空切割，不 需要进行分子蒸馏，简单可靠。
进一步的，油液固体分离设备具体采用离心机，结构简单，成本低。
进一步的，多级减压塔采用三段减压塔或者为三个单减压塔依次串联。
附图说明
图1为本发明实施例中废矿物油工艺框图。
图2为本发明实施例中系统结构示意图。
图中，1、油液固体分离设备；2、脱水塔；3、多级减压塔；4、储液槽。
具体实施方式
下面结合附图对本发明做进一步详细描述：
如图1所示，一种废矿物油分离处理方法，包括以下步骤：
步骤1)、对待处理废矿物油进行预处理脱除固体；废矿物油自原料罐区 通过泵送入离心机分离设备进行预处理，将废矿物油中的固体废物脱除；
步骤2)、将预处理后的废矿物油在100℃-200℃下进行初馏分离，去除 粗油和水分；
具体的，将预处理后的废矿物油加热至100℃-200℃送入脱水塔，废矿 物油在入脱水塔的塔顶将水分和低沸点的粗油蒸出，水份经凝后废水送污水 处理，低沸点的粗油送进罐区。脱水塔塔顶压力为常压或者负压。
步骤3)、将初馏分离后的废矿物油经过加热至260℃-300℃经过多级减 压蒸馏，将减压蒸馏后的气相产物换热冷凝形成液体产物，将液体产物通过 溶剂萃取精制得到符合标准的润滑油基础油。
所述溶剂采用糠醛、苯酚、N-二甲基酰胺或N-甲基吡咯烷酮。
具体采用加热方式为导热油、熔盐炉或者燃料气加热炉；最优采用导热 油加热，结构简单，能够最大利用初馏和闪蒸后余热。
将最后一级减压蒸馏后的塔釜产品送至真空脱焦系统进一步分离。
如图2所示，一种废矿物油分离处理系统，包括油液固体分离设备1、 脱水塔2和多级减压塔3，液固体分离设备1的液体出料口与脱水塔2入料 口通过加热管道连通，脱水塔2的液体出料口与多级减压塔3的入料口通过 加热管道连通，多级减压塔3的气相出口通过冷却管道连通至储液槽4，多 级减压塔3的塔釜产品出口连接至塔釜产品存储罐。脱水塔2的气相出口通 过冷凝管连接至冷凝处理。
油液固体分离设备1具体采用离心机。脱水塔2与多级减压塔3之间设 有初馏塔，用于对脱水塔处理后的液体进一步去粗油处理，提高液体提纯率。
本申请多级减压塔3采用三段减压塔或者为三个单减压塔依次串联。三 段减压塔内的三段压力分别为2.5-12.5KPaA、0.5-2.5KPaA、0.1-0.5KPaA； 三个单减压塔依次串联中第一级单减压塔的压力为2.5-12.5KPaA，第二级单 减压塔的压力为0.5-2.5KPaA，第三级单减压塔的压力为0.1-0.5KPaA。
以下采用具体的实施例进一步详细说明本发明，但本发明并不限于以下 实施例中公开的内容。
实施例1
废矿物油自原料罐区通过泵送入离心机进行离心分离，将废矿物油中的 固体废物脱除。废矿物油随后经加热至140℃进入常压脱水塔，塔顶将水份 和低沸点的粗油蒸出，冷凝后废水送污水处理，粗油进罐区；
脱水塔底部废矿物油经导热油加热至300℃，进入三段塔的第一级单减 压塔，在5KPaA操作压力下，废矿物油在第一级单减压塔发生闪蒸，第一级 单减压塔塔顶气相经换热冷凝后送至中间罐一，塔釜产品由泵抽出后经导热 油加热至310℃送至第二级单减压塔蒸馏分离；第二级单减压塔塔顶操作压 力为1KPaA，第二级单减压塔塔顶气相经换热冷凝后送至中间罐二，塔釜产 品由泵抽出后经导热油加热至320℃送至第三级单减压塔进行蒸馏分离，第 三级单减压塔塔顶操作压力为0.2KPaA，第三级单减压塔塔顶气相经换热冷 凝后送至中间罐三，塔釜产品由泵抽出后送至真空脱焦系统进一步分离。
减压蒸馏分离得到150SN、250SN、350SN的基础油进不同中间罐产品， 随后进入溶剂精制系统进一步萃取精制，从而得到符合标准的润滑油基础油。
实施例2
废矿物油自原料罐区通过泵送入离心机进行离心分离，将废矿物油中的 固体废物脱除。
废矿物油随后经与脱水塔及减压塔的采出换热，然后加热至160℃进入 常压脱水塔，塔顶将水份和低沸点的粗油蒸出，冷凝后废水送污水处理，粗 油进罐区。
脱水塔底部废矿物油经经导热油加热至260℃，进入三段塔的第一级单 减压塔，在6KPaA操作压力下，废矿物油在减压一塔发生闪蒸，塔顶气相经 换热冷凝后送至中间罐一，废矿物油在第一级单减压塔发生闪蒸，第一级单 减压塔塔顶气相经换热冷凝后送至中间罐一，塔釜产品由泵抽出后经导热油 加热至280℃送至第二级单减压塔蒸馏分离；第二级单减压塔塔顶操作压力 为1.2KPaA，塔顶气相经换热冷凝后送至中间罐二，第二级单减压塔塔顶气 相经换热冷凝后送至中间罐二，塔釜产品由泵抽出后经导热油加热至300℃送至第三级单减压塔进行蒸馏分离，第三级单减压塔塔顶操作压力为 0.2KPaA，塔顶气相经换热冷凝后送至中间罐三，塔釜产品由泵抽出后送至 真空脱焦系统进一步分离。
减压蒸馏分离得到150SN、250SN、350SN的基础油进不同中间罐产品， 随后进入溶剂精制系统进一步萃取精制，从而得到符合标准的润滑油基础油。
实施例3
废矿物油自原料罐区通过泵送入离心机进行离心分离，将废矿物油中的 固体废物脱除。
废矿物油随后经与脱水塔及减压塔的采出换热，然后加热至180℃进入 常压脱水塔，塔顶将水份和低沸点的粗油蒸出，冷凝后废水送污水处理，粗 油进罐区。
脱水塔底部废矿物油经导热油加热至300℃，进入三段塔的第一级单减 压塔，在10KPaA操作压力下，废矿物油在第一级单减压塔发生闪蒸，塔顶 气相经换热冷凝后送至中间罐一，塔釜产品由泵抽出后经导热油加热至320℃ 送至第二级单减压塔进行蒸馏分离，第二级单减压塔塔顶操作压力为2KPaA， 塔顶气相经换热冷凝后送至中间罐二，塔釜产品由泵抽出后经导热油加热至 330℃送至第三级单减压塔进行蒸馏分离，第三级单减压塔塔顶操作压力为 0.4KPaA，塔顶气相经换热冷凝后送至中间罐三，塔釜产品由泵抽出后送至真空脱焦系统进一步分离。
减压蒸馏分离得到150SN、250SN、350SN的基础油进不同中间罐产品， 随后进入溶剂精制系统进一步萃取精制，从而得到符合标准的润滑油基础油。
尽管上文已结合实施例对本发明的具体实施方式进行了详细描述，但是 需要指明的是，本发明的保护范围并不受这些具体实施方式的限制，而是由 权利要求书来确定。本领域技术人员可以依据本发明的技术构想对上述实施 方式进行各种等效改变和适当修改，其所产生的功能作用仍未超出说明书所 涵盖的精神时，均应在本发明的保护范围之内。
Claims (10)
1.一种废矿物油分离处理方法，其特征在于，包括以下步骤：
步骤1)、对待处理废矿物油进行预处理脱除固体；
步骤2)、将预处理后的废矿物油在100℃-200℃下进行初馏分离，去除粗油和水分；
步骤3)、将初馏分离后的废矿物油经过加热至260℃-300℃经过多级减压蒸馏，将减压蒸馏后的气相产物换热冷凝形成液体产物，将液体产物通过溶剂萃取精制得到符合标准的润滑油基础油。
2.根据权利要求1所述的一种废矿物油分离处理方法，其特征在于，废矿物油自原料罐区通过泵送入离心机分离设备进行预处理，将废矿物油中的固体废物脱除。
3.根据权利要求1所述的一种废矿物油分离处理方法，其特征在于，具体的，将预处理后的废矿物油加热至100℃-200℃送入脱水塔，废矿物油在入脱水塔的塔顶将水分和低沸点的粗油蒸出，水份经凝后废水送污水处理，低沸点的粗油送进罐区。
4.根据权利要求1所述的一种废矿物油分离处理方法，其特征在于，脱水塔塔顶压力为常压或者负压。
5.根据权利要求1所述的一种废矿物油分离处理方法，其特征在于，所述溶剂采用糠醛、苯酚、N-二甲基酰胺或N-甲基吡咯烷酮。
6.根据权利要求1所述的一种废矿物油分离处理方法，其特征在于，采用加热方式为导热油、熔盐炉或者燃料气加热炉。
7.一种废矿物油分离处理系统，其特征在于，包括油液固体分离设备(1)、脱水塔(2)和多级减压塔(3)，液固体分离设备(1)的液体出料口与脱水塔(2)入料口通过加热管道连通，脱水塔(2)的液体出料口与多级减压塔(3)的入料口通过加热管道连通，多级减压塔(3)的气相出口通过冷却管道连通至储液槽，多级减压塔(3)的塔釜产品出口连接至塔釜产品存储罐。
8.根据权利要求7所述一种废矿物油分离处理系统，其特征在于，脱水塔(2)的气相出口通过冷凝管连接至冷凝处理。
9.根据权利要求7所述一种废矿物油分离处理系统，其特征在于，油液固体分离设备(1)具体采用离心机。
10.根据权利要求7所述一种废矿物油分离处理系统，其特征在于，多级减压塔(3)采用三段减压塔或者为三个单减压塔依次串联。
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| CN112159705A (zh) * | 2020-09-29 | 2021-01-01 | 甘肃环馨新能源科技有限公司 | 一种废矿物油再生生产工艺 |
| CN112574771A (zh) * | 2020-12-09 | 2021-03-30 | 平遥同妙机车有限公司 | 基础油减压蒸馏工艺 |
| CN113105937A (zh) * | 2021-04-14 | 2021-07-13 | 中国恩菲工程技术有限公司 | 废矿物油的处理系统及处理方法 |
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