CN110194968B - 一种废润滑油全组分悬浮床加氢再生工艺 - Google Patents
一种废润滑油全组分悬浮床加氢再生工艺 Download PDFInfo
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- CN110194968B CN110194968B CN201910362008.5A CN201910362008A CN110194968B CN 110194968 B CN110194968 B CN 110194968B CN 201910362008 A CN201910362008 A CN 201910362008A CN 110194968 B CN110194968 B CN 110194968B
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- 239000010687 lubricating oil Substances 0.000 title claims abstract description 49
- 239000000725 suspension Substances 0.000 title claims abstract description 42
- 239000002699 waste material Substances 0.000 title claims abstract description 32
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 28
- 238000000034 method Methods 0.000 title claims abstract description 20
- 230000008929 regeneration Effects 0.000 title claims abstract description 13
- 238000011069 regeneration method Methods 0.000 title claims abstract description 13
- 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 35
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- 239000007789 gas Substances 0.000 claims description 35
- 229910052739 hydrogen Inorganic materials 0.000 claims description 10
- 239000001257 hydrogen Substances 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 239000003054 catalyst Substances 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N hydrogen Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 6
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- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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- 239000000126 substance Substances 0.000 description 1
- 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
Classifications
-
- 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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
-
- 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润滑油全组分悬浮床加氢再生工艺，包括以下步骤：1），首先进行预处理；2），将预处理后的废润滑油进行悬浮床加氢反应；3），将反应产物进入悬浮床热高压分离器进行气相与液相分离，气体产物在悬浮床冷高压分离器中分离出气相、酸性水和液相；4），步骤3）中液相经减压进入悬浮床热低压分离器分离，闪蒸出来的气体进入汽提塔，底部出来的浆液升温后进入减压塔，汽提塔气体经冷却后分离出不凝气、酸性水和溶剂油；5），减压塔通过减压分离出溶剂油和润滑油基础油，减压塔底分离出沥青产品。本发明能够更好地对废润滑油进行再利用处理，不但成本低廉，而且回收率高，安全、环保。
Description
技术领域
本发明涉及环保技术领域，特别是涉及一种废润滑油全组分悬浮床加氢再生工艺。
背景技术
目前我国对润滑油的需求逐年增加，然而当润滑油使用一段时间后，由于化学、物理等因素使其各项性能指标不断劣化，当达到一定程度时就不能再继续使用，就必须换油，因此产生大量的废润滑油，造成环境污染。实际上废润滑油只是其中极少一部分物质因生成了醛、酮、胶质、碳黑等，同时带进了水、机械杂质等，发生了变质，而大部分组分并未发生变质，可以通过一些处理手段再生。目前废润滑油的再生工艺主要有两种：一种是蒸馏—酸洗—白土精制，沉降—酸洗—蒸馏—白土精制，蒸馏—糠醛精制—白土精制等物理工艺，这种工艺润滑油回收率低、产生大量固体废弃物和酸渣，环境污染大。另一种是采用固定床加氢精制工艺，首先对废润滑油进行脱水脱杂处理，处理后的废润滑油进行脱重处理，除去原料中的胶质及沥青质，分离出废润滑油中的轻质组分进行加氢，最后得到一部分润滑油基础油，该工艺仅仅对废润滑油部分组分加氢，而非全组分加氢，润滑油回收率低；同时采用Ni—Mo系贵金属催化剂，催化剂价格昂贵，同时原料适应性较差，更换时间短，故该工艺相对复杂、润滑油回收率低、操作成本高，没有竞争优势。
发明内容
本发明所要解决的技术问题就是针对上述背景技术的不足，提供一种废润滑油全组分悬浮床加氢再生工艺，在实现废润滑油充分利用的前提下，满足节能、环保、成本低廉的要求。
为解决上述技术问题，本发明提供的一种废润滑油全组分悬浮床加氢再生工艺，包括以下步骤：
1），首先进行预处理，脱除去废润滑油中的机械杂质等无效组分及结焦、磨损组分，将废润滑油中的含水率降低到0.1~0.2%w；
2），将预处理后的废润滑油升压后与高压氢气混合，选用Fe系催化剂浆液催化，在悬浮床反应器进行加氢反应；
3），悬浮床加氢反应产物进入悬浮床热高压分离器进行气相与液相分离，气体产物降温后进入悬浮床热高分气空冷器冷却，而后在悬浮床冷高压分离器中分离出气相、酸性水和液相；
4），步骤3）中液相经减压进入悬浮床热低压分离器分离，闪蒸出来的气体进入汽提塔，底部出来的浆液升温后进入减压塔，汽提塔气体经冷却后分离出不凝气、酸性水和溶剂油；
5），减压塔通过减压分离出溶剂油和润滑油基础油，减压塔底分离出沥青产品。
在上述技术方案中，所述步骤2）中，加氢反应反应温度300~380℃，反应压力4~10MPa。
在上述技术方案中，所述步骤2）中，加氢反应氢油体积比400~1000，体积空速0.1~0.5h-1。
在上述技术方案中，所述步骤4）中，气体产物依次与混合原料、混氢、悬浮床冷低分液换热后进入悬浮床热高分气空冷器冷却。
在上述技术方案中，所述步骤5）中减压塔塔顶设置抽真空系统，塔顶气经冷却后进入减压塔顶罐，不凝气经水封罐水封后送至减压塔加热炉燃烧，酸性水送至酸性水罐，污油经泵升压后送至污油罐。
与现有技术相比，本发明的有益效果在于：1）实现了废润滑油全组分加氢；2）润滑油基础油回收率95%以上，收率高；3）产品质量高，硫、氮及芳烃含量低，黏度指数高，热氧化安定性好，挥发性低；4）工艺流程简单，操作灵活性大，安全、可靠性高；5）生产过程无酸碱废弃物排放，环保无污染。
附图说明
图1为本发明工艺流程示意图。
具体实施方式
以下结合附图对本发明的具体实施例作进一步的详细描述：
如图1所示，本发明提供的一种废润滑油全组分悬浮床加氢再生工艺，包括以下步骤：
1），首先进行预处理，脱除去废润滑油中的机械杂质等无效组分及结焦、磨损组分，将废润滑油中的含水率降低到0.1~0.2%w；
2），将预处理后的废润滑油升压后与高压氢气混合，选用Fe系催化剂浆液催化，在悬浮床反应器进行加氢反应；
3），悬浮床加氢反应产物进入悬浮床热高压分离器进行气相与液相分离，气体产物降温后进入悬浮床热高分气空冷器冷却，而后在悬浮床冷高压分离器中分离出气相、酸性水和液相；
4），步骤3）中液相经减压进入悬浮床热低压分离器分离，闪蒸出来的气体进入汽提塔，底部出来的浆液升温后进入减压塔，汽提塔气体经冷却后分离出不凝气、酸性水和溶剂油；
5），减压塔通过减压分离出溶剂油和润滑油基础油，减压塔底分离出沥青产品。
具体地，所述步骤1）中，通过预处理脱除去废润滑油中的机械杂质等无效组分及结焦、磨损组分。
所述步骤2）反应参数优选：反应温度300~380℃，反应压力4~10MPa，氢油体积比400~1000，体积空速0.1~0.5h-1。由于反应为放热反应，反应器温度将会升高，反应器应设有冷氢口、急冷油口以控制反应温度。
所述步骤4）中，悬浮床加氢反应产物进入悬浮床热高压分离器进行气相与液相分离。气体产物依次与混合原料、混氢、悬浮床冷低分液换热后进入悬浮床热高分气空冷器冷却，后进入悬浮床冷高压分离器，分离出气相、酸性水和液相。悬浮床热高分底部的浆液相经减压，进入悬浮床热低压分离器分离，闪蒸出来的气体进入汽提塔。悬浮床热低压分离器底部出来的浆液经减压塔加热炉升温后进入减压塔。悬浮床冷高压分离器顶气体去循环氢分液罐，酸性水送至酸性水罐。
所述步骤5）中，汽提塔塔顶气体经冷却后进入汽提塔顶回流罐，分离出不凝气、酸性水和溶剂油，汽提塔干气至干气脱硫，酸性水至酸性水罐。汽提塔底的润滑油基础油送至罐区。减压塔塔顶设置抽真空系统，塔顶气经冷却后进入减压塔顶罐，不凝气经水封罐水封后送至减压塔加热炉燃烧，酸性水送至酸性水罐，污油经泵升压后送至污油罐。减压塔通过减压分离出溶剂油和润滑油基础油，减压塔底分离出沥青产品。
本发明的核心是利用Fe为催化剂，通过加氢反应处理废润滑油，并且通过对加氢反应后的产物细致处理得到溶剂油、润滑油基础油、沥青和酸性水等产物，因此，本发明的保护范围不仅限于上述实施例，在本发明原理的基础上，任何利用上述机理的改变或变形，均属于本发明的保护范围。
Claims (5)
1.一种废润滑油全组分悬浮床加氢再生工艺，其特征在于包括以下步骤：
1），首先进行预处理，脱除去废润滑油中的机械杂质及结焦、磨损组分，将废润滑油中的含水率降低到0.1~0.2 wt %；
2），将预处理后的废润滑油升压后与高压氢气混合，选用Fe系催化剂浆液催化，在悬浮床反应器进行加氢反应；
3），悬浮床加氢反应产物进入悬浮床热高压分离器进行气相与液相分离，气体产物降温后进入悬浮床热高分气空冷器冷却，而后在悬浮床冷高压分离器中分离出气相、酸性水和液相；
4），步骤3）中经悬浮床热高压分离器分离得到的液相经减压进入悬浮床热低压分离器分离，闪蒸出来的气体进入汽提塔，底部出来的浆液升温后进入减压塔，汽提塔气体经冷却后分离出不凝气、酸性水和溶剂油；
5），减压塔通过减压分离出溶剂油和润滑油基础油，减压塔底分离出沥青产品。
2.根据权利要求1所述的废润滑油全组分悬浮床加氢再生工艺，其特征在于：所述步骤2）中，加氢反应反应温度300~380℃，反应压力4~10MPa。
3.根据权利要求1或2所述的废润滑油全组分悬浮床加氢再生工艺，其特征在于：所述步骤2）中，加氢反应氢油体积比400~1000，体积空速0.1~0.5h-1。
4.根据权利要求1或2所述的废润滑油全组分悬浮床加氢再生工艺，其特征在于：所述步骤5）中减压塔塔顶设置抽真空系统，塔顶气经冷却后进入减压塔顶罐，不凝气经水封罐水封后送至减压塔加热炉燃烧，酸性水送至酸性水罐，污油经泵升压后送至污油罐。
5.根据权利要求3所述的废润滑油全组分悬浮床加氢再生工艺，其特征在于：所述步骤5）中减压塔塔顶设置抽真空系统，塔顶气经冷却后进入减压塔顶罐，不凝气经水封罐水封后送至减压塔加热炉燃烧，酸性水送至酸性水罐，污油经泵升压后送至污油罐。
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