CN100503796C - 一种废润滑油的再生方法 - Google Patents
一种废润滑油的再生方法 Download PDFInfo
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- CN100503796C CN100503796C CNB2007100542274A CN200710054227A CN100503796C CN 100503796 C CN100503796 C CN 100503796C CN B2007100542274 A CNB2007100542274 A CN B2007100542274A CN 200710054227 A CN200710054227 A CN 200710054227A CN 100503796 C CN100503796 C CN 100503796C
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- oil
- lubricating oil
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- tower
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- 239000002699 waste material Substances 0.000 title claims abstract description 66
- 239000010687 lubricating oil Substances 0.000 title claims description 87
- 238000011069 regeneration method Methods 0.000 title abstract description 15
- 239000012535 impurity Substances 0.000 claims abstract description 23
- 238000004821 distillation Methods 0.000 claims abstract description 20
- 238000007670 refining Methods 0.000 claims abstract description 19
- 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 12
- OFBQJSOFQDEBGM-UHFFFAOYSA-N pentane Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims abstract description 4
- 239000003921 oil Substances 0.000 claims description 117
- 239000000463 material Substances 0.000 claims description 30
- 239000002904 solvent Substances 0.000 claims description 26
- 239000002253 acid Substances 0.000 claims description 17
- 238000000034 method Methods 0.000 claims description 16
- 238000000526 short-path distillation Methods 0.000 claims description 14
- 238000005292 vacuum distillation Methods 0.000 claims description 11
- 239000004519 grease Substances 0.000 claims description 10
- 239000004215 Carbon black (E152) Substances 0.000 claims description 9
- 239000002283 diesel fuel Substances 0.000 claims description 9
- 239000003795 chemical substances by application Substances 0.000 claims description 7
- 238000005189 flocculation Methods 0.000 claims description 7
- 230000016615 flocculation Effects 0.000 claims description 6
- 238000005119 centrifugation Methods 0.000 claims description 5
- 241000282326 Felis catus Species 0.000 claims description 4
- 238000009835 boiling Methods 0.000 claims description 3
- 150000002430 hydrocarbons Chemical class 0.000 claims description 3
- 238000009418 renovation Methods 0.000 claims description 3
- 238000010792 warming Methods 0.000 claims description 3
- 239000000314 lubricant Substances 0.000 abstract description 12
- 230000008929 regeneration Effects 0.000 abstract description 11
- 239000000126 substance Substances 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 29
- 230000001264 neutralization Effects 0.000 description 15
- 239000002199 base oil Substances 0.000 description 14
- 238000004519 manufacturing process Methods 0.000 description 14
- HYBBIBNJHNGZAN-UHFFFAOYSA-N Furfural Chemical compound 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- 239000000047 product Substances 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical group 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OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
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CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 1
- SECXISVLQFMRJM-UHFFFAOYSA-N n-methylpyrrolidone Chemical compound 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CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N phenol Chemical compound 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Abstract
本发明公开了一种废润滑油的再生方法。其方法是废润滑油自然沉降,脱除其含有的水和机械杂质,当废润滑油中的机械杂质含量低于0.08重量%或戊烷不溶物小于0.30重量%时,直接进行常减压蒸馏,否则向其中加入占废润滑油总重量0~3.5倍的稀释剂,升温至30℃~95℃,进行分离后再进行常减压蒸馏,经常减压蒸馏的废润滑油,再进行短程蒸馏和润滑油料精制,即得再生后润滑油。使用本发明方法进行废润滑油的再生,无酸渣排放,且副产品都可直接利用,工艺过程符合环保要求。
Description
一种废润滑油的再生方法
技术领域
本发明属于从废料中回收脂油,特别涉及一种废润滑油的再生方法。 背景技术
随着国民经济的快速增长和轿车工业的快速发展,国内对润滑油的需求量
越来越大,据统计2005年国内消售润滑油550万吨左右。润滑油在使用过禾呈中, 在高温、高压等条件下裂解、縮合;与空气接触氧化变质,在某些金属的f崔化 作用下,使氧化加剧;同时添加剂的分解、破坏,失去添加剂原有的作用;以 及从外界还混入轻质油、灰尘和金属削等杂质,从而使润滑油失去了原有的某 些性能,其使用性能变差,满足不了使用要求,故应对其更换,换下来的润滑 油一般称为废润滑油或废油。
尽管润滑油在使用过程中会消耗一些,但是绝大部分润滑油用过后经再生 加工可重新利用。对废润滑油进行再生,不仅能节约有限的石油资源,而且对 保护环境也有十分重要意义。因此,国内外开发了多种废润滑油的再生技术。
国外的废润滑油再生工艺主要有:
Snampmgetti工艺:废油先经常压蒸馏,脱去水和轻质油后去丙垸抽提,丙 烷抽出油再经减压蒸馏获得润滑油料组分和残油,该残油再用丙烷抽提得残油 料润滑油组分,润滑油组分和残油料润滑油组分全部去加氢精制得到润滑油的 基础油。该工艺已工业化,生产的产品质量符合中性基础油的质量标准,但投 资较高。
KTI工艺:废油先沉降,再经常压、减压蒸馏,获得润滑油料组分和残油,
占废润滑油80111%-85111%的润滑油料组分去加氢精制得到润滑油的基础油。该工 艺也已工业化,生产的产品质量符合中性基础油的质量标准,但投资也较高。
DUH工艺。该工艺为UOP公司开发的技术,废润滑油直接加氢处理,以获 得包括轻、重润滑油料的各种石油产品,其中润滑油的产率为60m^左右。采用 该技术的装置投资较高。
REG工艺。该工艺采用闪蒸、热处理、超细过滤、加氢精制、减压蒸馏来 再生润滑油。产品总收率在86my。左右,产品质量符合中性基础油的质量标准, 但投资较高。
IFP工艺。该工艺为法国石油研究院开发。废润滑油经丙烷萃取除去其主要 杂质后,再进行H2S04精制和白土精制。但由该工艺再生润滑油会对环境造成 一定的污染。
BERC工艺。该工艺为美国能源部能源研究中心开发。该工艺采用混合溶剂(正丁醇:异丙醇:甲乙酮=2: 1: 1)对废润滑油进行萃取,并用离心法除去 杂质,脱除溶剂后的精制油再经过减压蒸馏,得到的减压润滑油料再加氢精制 或白土精制以得到润滑油组分。采用该工艺的装置投资较高。
Recyckm工艺。该工艺用细粉状金属钠与废润滑油反应,以除去油中的氧 化物和添加剂;采用常压蒸馏除去反应物,再采用3个薄膜分子蒸馏塔来得到 润滑油组分。但该工艺使用细粉状金属钠,很容易自然,要求装置有较高的安 全性。
国外开发的废润滑油再生技术以无污染或低污染为主,充分体现了环境保 护的重要性。而国内受废润滑油的收集困难,加工分散,只重视眼前利益影响, 多采用落后的有酸再生工艺(如蒸馏一酸洗一白土精制工艺、沉淀一酸洗一白 土精制工艺、沉淀一蒸馏一酸洗一白土精制工艺等)来处理废润滑油,这给当 地的环境造成了严重影响。
随着国内对环境保护的日益重视,国内也相继开发了低污染或无污染的废 润滑油再生技术。
中国专利CN96119130.9公布了废油再生白土高温精制工艺及装置。该工艺 首先将废油、白土、汽三相混输,在管式炉循环精制蒸馏釜中加热到30(TC,闪 蒸出水分、轻柴油;然后带土油转到第二座管式炉循环精制蒸馏釜,油、白土、 汽三相在剧烈的紊流状态下加热精制到40(TC,最后换热降温至13(TC后过滤, 得到中性油和光亮油。该工艺较为简单,对环境影响小,但加入的白土量较大 (〉10m%),设备的磨损严重,尤其装置在运行后期,炉管有被堵塞的可能;
且油品在高温下会发生裂解,使得中性油和光亮油的氧化安定性较差。
中国专利CN91110965.X、 CN92111245.9、 CN85100831和CN94116740.2
各公布了絮凝法再生废润滑油的方法。这些再生工艺的流程简单,无环境污染 或环境污染小,但油品的质量较差,且存在絮凝剂不通用等问题。
中国专利CN00123153.7和CN01106012.3各公布了一种废油的回收方法, 其主要工艺采用悬浮床加氢工艺。采用加氢工艺处理废润滑油,得到的再生中 性油和副产品轻质油的质量好,生产过程无环境污染;但装置的投资高,且目 前在国内还没有采用该类方法的生产装置报道。
另外,中国专利CN99103452.X、 CN200410026034.4以及国夕卜(加拿大) 在中国申请的专利CN97193273.5等公布了利用废油生产燃料油的方法。这些方 法对环境的影响较小,但有限的石油资源没有得到合理的使用。
发明内容
本发明为了合理利用有限的石油资源,解决废润滑油再生过程中存在的工 艺不足以及废润滑油再生装置投资较高等问题,提供了一种新的废润滑油再生方法。使用本发明方法再生后的润滑油质量好,对环境无污染。 本发明提供的废润滑油再生方法包括以下步骤:
1) 废润滑油的去杂质:废润滑油自然沉降,脱除其含有的水和机械杂质, 当废润滑油中的机械杂质含量低于O. 08重量%或戊垸不溶物小于0. 30重量%时,
直接进入步骤2),否则向其中加入占废润滑油总重量0〜3. 5倍,优选1. 0倍〜 2.0倍的稀释剂,升温至30。C〜95。C,优选35。C〜65。C,进行离心分离,机械 杂质含量满足上述要求后进入步骤2)。所述稀释剂由以稀释剂总重量计含0〜 5. 0重量%絮凝剂和95. 0〜100重量%的沸程为60〜20(TC的烃油馏分组成;所述 烃油馏分优选90号溶剂油、120号溶剂油或200号溶剂油等。所述絮凝剂为本 领域普通技术人员所熟知的聚醚类或酰胺类。
2) 常、减压蒸馏:来自步骤l)的脱杂质的废润滑油进入常压塔在常压蒸
馏条件下蒸馏出20(TC以下馏分,循环到步骤l)作为稀释剂;常压塔的塔底油
进入减压塔,在减压蒸馏条件下,减压塔的塔顶出柴油馏分或轻柴油馏分,侧
线出30(TC〜37(TC重柴油馏分或/和37(rC〜45(rC轻质润滑油料,重柴油馏分 和轻质润滑油料进入步骤4),减压塔的塔底油进入步骤3);
3) 短程蒸馏:来自步骤2)的减压塔塔底油在1〜650Pa,优选3〜133Pa 的压力下,加热到20(TC〜35(TC,优选20(rC〜32(TC进行短程蒸馏,得到370 。C〜450。C轻质润滑油料、450。C〜50(TC的中质润滑油料和500。C〜560。C或500 "C〜58(TC的重质润滑油料,轻质润滑油料、中质润滑油料和重质润滑油料进入 步骤4);
4) 润滑油料精制:来自步骤2)重柴油馏分在常规白土精制条件下精制得 润滑油;来自步骤2)和步骤3)的轻质润滑油料、中质润滑油料和重质润滑油 料分别进行精制,当其酸值为小于或等于0. 10mgKOH/g时,在白土精制条件下精制 得润滑油;当其酸值为大于0. 10mgK0H/g时,在溶剂精制和白土精制 条件下精制得润滑油。
本发明所述的溶剂精制工艺选择的溶剂为本领域技术人员熟知的溶剂,如 糠醛、苯酚和N—甲基吡咯烷酮等。以糠醛为溶剂时,轻质润滑油料在抽提温 度为5CTC〜13(TC,溶剂与轻质润滑油料的重量比为1. 2〜2. 5的条件下进行精 帝ij;中质润滑油料在抽提温度为65。C〜135。C,溶剂与中质润滑油料的重量比 为1.5〜3.0的条件下进行精制;重质润滑油料在抽提温度为7(TC〜145"C,溶 剂与重质润滑油料的重量比为2.0〜4.0的条件下进行精制;步骤2)的重柴油 馏分在抽提温度为7(TC〜145°C,溶剂与重柴油馏分的重量比为0.8〜2.0的条 件下进行精制。
本发明所述润滑油料进行白土精制时,白土的加入量(占原料)为2〜8重量%,操作温度120〜280°C,停留时间为20〜60分钟。
本发明处理的废润滑油是指废内燃机油、废机械油、废变压器油、废冷冻 机油、废汽轮机油、废真空泵油、废导轨油、废电梯用油或废压缩机油等。
由步骤(2)得到的柴油馏分(16(TC〜37(TC馏分油、或16(〕°C〜320。C馏 分油、或20CTC〜37(TC馏分油、或2(XrC〜320。C馏分油)可作为轻燃料油4吏用, 或作为生产柴油的掺兑料。由步骤(3)得到的残油可作为重燃料油或重燃料油 的调和组分。由步骤(4)得到的溶剂精制抽出油直接作为燃料油或其它产品如 橡胶充油等使用;得到的含油白土可作为烧砖的原料等。因此,该工艺过禾呈对 环境基本不造成影响。
本发明与现有技术相比具有以下优点:
1. 废润滑油再生过程无酸渣排放,其副产品都可直接利用,工艺过程f守合 环保要求;
2. 本发明采用的工艺技术路线灵活,可处理各种废润滑油;
3. 产品的综合商品率在90%以上;
4. 再生油的酸值低,色号小,抗氧化安定性好,各项技术指标符合润^"油 基础油的质量要求;
5. 与加氢精制工艺相比,投资较低。 附图说明
图是本发明废润滑油再生方法的一种简单流程图。
图中:1—废润滑油;2—水和机械杂质;3—稀释剂;4—絮凝剂;5—油 膏;6—水;7—轻柴油馏分或柴油馏分;8—重柴油馏分或重柴油馏分和轻质润 滑油料;9一轻、中、重质润滑油料或中、重质润滑油料;10--残油;ll一溶剂 (如糠醛);12—白土; 13—含油白土; 14、 15、 16、 17—中性基础油;18—去 杂质单元;19一常减压蒸馏;20—短程蒸馏;21—精制单元。
如图所示,废润滑油l进入去杂质单元18,先自然沉降,脱除其含有的部 分水和机械杂质2,当废润滑油的机械杂质含量低于0. 08itf/。或戊烷不溶物小于 0.30my。时,直接去常减压蒸馏装置;否则向脱除部分水和机械杂质的废润滑油 中加入占废润滑油总重量该0〜3..5倍的稀释剂3,优选i. 0倍〜2. 0倍的稀释 齐U,升温至3(TC〜95。C,优选35。C〜65'C,在搅拌釜中混合均匀(或通过静态 混合器使油样混合均匀),经20〜40分钟的沉降后再经离心分离或过滤,得到 油膏5,去掉杂质的混合油样加热到18(rC〜26(TC后去常减压蒸馏装置19。其 中所述稀释剂为加入占稀释剂总重量0%〜5. 0%絮凝剂4后的稀释剂,稀释剂为 包括烃类溶剂油在内的沸点小于200。C的汽油馏分,优选90号溶剂油、120号 溶剂油和200号溶剂油等。所述絮凝剂为本领域普通技术人员所熟知的聚醚类或酰胺类。
废润滑油在常压蒸馏装置19中先在常压塔中进行常压蒸馏,蒸馏出稀释剂 3和水分6。汽油馏分一部分循环到去杂质工序,剩余部分出装置。常压塔底油 再加热到200°C〜350°C ,优选22(TC〜320。C进入减压蒸馏塔,在650Pa〜24KPa, 优选1. 33Kpa〜13. 3KPa的残压下进行蒸馏分离。该减压蒸馏塔上至少有一个侧
线,其底部有适量的水蒸汽吹入。减压蒸馏塔塔顶出如小于3oor的轻柴油馏
分或柴油馏分7;而减压塔的侧线应根据废润滑油窄馏分油的性质和收率等来 决定是否抽出如30(TC〜37(TC的重柴油馏分8或重柴油馏分和如370°C〜450
t:的轻质润滑油料8。
出减压塔的塔底油被加热到200°C〜350°C,优选20(TC〜32(TC进入多级 (至少2级)串级的短程蒸馏20 (或称分子蒸馏、薄膜蒸发等)设备中,每一 级短程蒸馏设备均有加热介质(导热油或导热液等)和冷却介质(导热油或循 环水等)。在lPa〜650Pa,优选3Pa〜133Pa的残压下,经三级短程蒸馏分别 得到润滑油料9,如37CrC〜45(TC的轻质润滑油料、45(TC〜50(TC的中质润滑 油料和500。C〜56(TC或500。C〜58(TC的重质润滑油料;而经两级短程蒸馏则得 到中质润滑油料和重质润滑油料。润滑油料去精制单元21,而最后一级得到的 的残油10出装置。
在润滑油料精制单元21中,根据润滑油料的性质如酸值、颜色等灵活选择 适宜的精制过程。当润滑油料的酸值为0. 10mgK0H/g以下时,直接采用白土补 充精制;否则采用溶剂精制和白土补充精制以降低润滑油料的酸值、色度,使 其安定性提高。该单元采用适宜的溶剂11如糠醛和适宜的操作条件先对不同润 滑油料进行溶剂精制;然后加入适量的白土 12在适宜的温度下进行补充精制, 过滤出含油白土 13得到润滑油的中性油14、 15、 16和17。
具体实施方式
以下用具体实施例对本发明进行详细说明,但并不限制本发明的使用范围。 实施例h
废润滑油A的性质见表1。该废润滑油100份经自然沉降后再加入150份 120号溶剂油,稀释均匀的混合油样加热到5(TC经离心分离进一.步分离出油中 的机械杂质。
分离出机械杂质的混合油样加热到23(TC经常压蒸馏蒸馏出〈20(TC的汽油 馏分(包括稀释剂),并脱除水分;〉20(TC的馏分在残压为650Pa的条件下加 热蒸馏出20(rC〜300。C馏分(作为轻质燃料油)、30(TC〜37(TC馏分(作为主轴 油的生产原料油)和370。C〜45(TC馏分(作为IOOSN的生产原料油);〉450°C 馏分加热到28(TC经一级短程蒸馏(降膜),在残压为40Pa的条件下切割出450。C〜52(TC馏分(作为350SN的生产原料油);〉52(TC馏分加热到30(TC经二级 短程蒸馏(降膜),在残压为6.5Pa的条件下切割出52(TC〜580。C馏分(作为 650SN的生产原料油),〉58(TC的残渣油作为重质燃料油。
300。C〜370。C馏分、37(TC〜45(TC馏分、450°C〜520。C馏分、520°C〜580 。C馏分经糠醛精制或经糠醛精制和白土精制分别得到N5主轴油、100SN、350SN 和650SN中性基础油。糠醛精制和白土精制的操作条件以及精制油的收率和性 质见表2。在表3中列出了中性基础油的质量标准。
表1废润滑油A的性质
项目名称 分析数据
密度(2(TC), kg/m3 885.1
运动粘度(50°C), mm2/s 24
粘度指数 112
残炭,m% 0.51
酸值,mgKOH/g 0.46
闪点(开),°c 91
水含量,m% 5.8
机械杂质,m% 0.62
灰分,m% 0.21
S, (ig/g 4630
N, (ag/g 361
金属分析,^g/g
Na 8.7
Cu 7.6
Fe 209
Pb 37
Zn 53
Ca 126
组成分析,m%
饱和烃 85.6
芳香烃 13.2
胶质 1.2
8表2废润滑油A窄馏分精制条件、收率及性质
<table>table see original document page 9</column></row>
<table>表3中性基础油的质量标准
<table>table see original document page 10</column></row>
<table>由表2和表3可知,除倾点外,各精制油均满足了中性基础油的质量标准。 而降低精制油的倾点可加入适量的降凝剂来实现。如450。C〜52(TC馏分的精制 油倾点为+2'C,但调入0.1m。/。的T801降凝剂可使其倾点降低到45t:。
糠醛抽出油可作为齿轮油,或饱和汽缸油,或燃料油等;含油白土作为烧 砖的原料。
实施例2:
废润滑油B的性质见表4。废润滑油B 100份经自然沉降后再加入200份 200号溶剂油,同时加入1.5份有机絮凝剂聚醚,混合油样加热到70°C,搅拌 30min,沉降1小时后经离心分离进一步分离出油中的机械杂质。 分离出机械杂质的混合油样加热到23(TC经常压蒸馏蒸馏出〈20(TC的汽油馏分 (包括稀释剂),并脱除水分;〉20(TC的馏分在残压为5KPa的条件下加热,减 压塔底吹入适量的水蒸汽,蒸馏出20(TC〜37(TC馏分(作为轻质燃料油);>370 。C馏分加热到235"C经一级短程蒸馏(降膜),在残压为133Pa的条件下切割出 370。C〜440。C馏分(作为100SN的生产原料油);〉440。C馏分加热到255。C经 二级短程蒸馏(降膜),在残压为40Pa的条件下切割出44(TC〜49(TC馏分(作 为200SN的生产原料油);〉4卯。C馏分加热到285。C经三级短程蒸馏(降膜), 在残压为8Pa的条件下切割出49(TC〜55(TC馏分(作为350SN的生产原料油), >560°C的残渣油作为重质燃料油。
370。C〜44(TC馏分、44(TC〜490。C馏分、490°C〜55(TC馏分经糠醛精制和 白土精制分别得到IOOSN、 200SN和350SN中性基础油。糠醛精制和白土精制 的操作条件以及精制油的收率和性质见表5。由表5数据对照表3可以看出,各精制油均满足了中性基础油的质量标准。抽出油和含油白土利用同实施例1。
表4 废润滑油B的性质
<table>table see original document page 11</column></row>
<table>表5废润滑油 <table>table see original document page 12</column></row>
<table>实施例3
废润滑油C的性质见表6。废润滑油C经自然沉降,分离出机械杂质,然 后加热到230。C经常压蒸馏蒸馏出〈20(TC的汽油馏分,并脱除水分;>200°(3的 馏分加热,在残压为4Kpa,减压塔底吹入适量水蒸汽的条件下,蒸馏出20(TC〜37(TC馏分(作为轻质燃料油)禾卩370。C〜45(TC馏分(作为100SN的生产原料 油);〉45(TC馏分加热到268t:经一级短程蒸馏(降膜),在残压为50Pa的条件 下切割出450。C〜50(TC馏分(作为150SN的生产原料油);>500°。馏分加*冉到 280。C经二级短程蒸馏(降膜),在残压为8Pa的条件下切割出50(TC〜54(TC馏 分(作为350SN的生产原料油),>540匸的残渣油作为重质燃料油。
370。C〜45(TC馏分、45(TC〜50(TC馏分、500°C〜54(TC馏分不经糠醛精制 而直接进行白土精制分别得到IOOSN、 150SN和350SN中性基础油。白土精制 的操作条件以及精制油的收率和性质见表7。由表7数据对照表3可以看出,各 精制油均满足了中性基础油的质量标准。抽出油和含油白土利用同实施例1。
表6 废润捐 <table>table see original document page 13</column></row>
<table>表7废润滑油C窄馏分精制条件、收率及性质
<table>table see original document page 14</column></row>
<table>
Claims (3)
1. 一种废润滑油的再生方法,其特征在于该方法包括以下步骤:1)废润滑油的去杂质:废润滑油自然沉降,脱除其含有的水和机械杂质,当废润滑油中的机械杂质含量低于0.08重量%或戊烷不溶物小于0.30重量%时,直接进入步骤2),否则向其中加入占废润滑油总重量0~3.5倍的稀释剂,升温至30℃~95℃,进行离心分离,机械杂质含量满足上述要求后进入步骤2);所述稀释剂由以稀释剂总重量计含0~5.0重量%絮凝剂和95.0~100重量%的沸程为60~200℃的烃油馏分组成;2)常、减压蒸馏:来自步骤1)的脱杂质的废润滑油进入常压塔在常压蒸馏条件下蒸馏出200℃以下馏分,循环到步骤1)作为稀释剂;常压塔的塔底油进入减压塔,在减压蒸馏条件下,减压塔的塔顶出柴油馏分或轻柴油馏分,侧线出300℃~370℃重柴油馏分或/和370℃~450℃轻质润滑油料,重柴油馏分和轻质润滑油料进入步骤4),减压塔的塔底油进入步骤3);3)短程蒸馏:来自步骤2)的减压塔塔底油在1~650Pa的压力下,加热到200℃~350℃,进行短程蒸馏,得到370℃~450℃轻质润滑油料、450℃~500℃的中质润滑油料和500℃~560℃或500℃~580℃的重质润滑油料,轻质润滑油料、中质润滑油料和重质润滑油料进入步骤4);4)润滑油料精制:来自步骤2)重柴油馏分在白土精制条件下精制得润滑油;来自步骤2)和步骤3)的轻质润滑油料、中质润滑油料和重质润滑油料分别进行精制,当其酸值小于或等于0.10mgKOH/g时,在白土精制条件下精制得润滑油;当其酸值大于0.10mgKOH/g时,在溶剂精制和白土精制条件下精制得润滑油。
2. 根据权利要求1所述的方法,其特征在于:步骤l)中稀释剂的加入量 为占润滑油总重量的1.0倍〜2.0倍。
3. 根据权利要求1所述的方法,其特征在于:步骤3)短程蒸馏的压力为 3〜133Pa, p度为200。C〜320。C。
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