CN107312568A - 一种废矿物油催化裂解综合利用系统及其加工工艺 - Google Patents
一种废矿物油催化裂解综合利用系统及其加工工艺 Download PDFInfo
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- CN107312568A CN107312568A CN201710500101.9A CN201710500101A CN107312568A CN 107312568 A CN107312568 A CN 107312568A CN 201710500101 A CN201710500101 A CN 201710500101A CN 107312568 A CN107312568 A CN 107312568A
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- oil
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- preheating
- tower
- catalytic
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- 239000002699 waste material Substances 0.000 title claims abstract description 51
- 238000007233 catalytic pyrolysis Methods 0.000 title claims abstract description 37
- 238000005516 engineering process Methods 0.000 title claims abstract description 20
- 239000003921 oil Substances 0.000 claims abstract description 119
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- 238000007701 flash-distillation Methods 0.000 claims abstract description 33
- 238000004065 wastewater treatment Methods 0.000 claims abstract description 30
- 238000004523 catalytic cracking Methods 0.000 claims abstract description 23
- 238000007781 pre-processing Methods 0.000 claims abstract description 21
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- 230000003197 catalytic Effects 0.000 claims description 52
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- 238000003860 storage Methods 0.000 claims description 9
- 238000000638 solvent extraction Methods 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 7
- 238000002156 mixing Methods 0.000 claims description 6
- WYURNTSHIVDZCO-UHFFFAOYSA-N tetrahydrofuran Chemical compound 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C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 claims description 6
- PNEYBMLMFCGWSK-UHFFFAOYSA-N al2o3 Chemical compound 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[O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 5
- 239000002283 diesel fuel Substances 0.000 claims description 5
- 238000011068 load Methods 0.000 claims description 5
- 239000002808 molecular sieve Substances 0.000 claims description 5
- 238000001514 detection method Methods 0.000 claims description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N methanol Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 4
- HYBBIBNJHNGZAN-UHFFFAOYSA-N Furfural Chemical compound 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O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 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
- -1 DAA Chemical compound 0.000 claims description 2
- 239000000498 cooling water Substances 0.000 claims description 2
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- 125000004836 hexamethylene group Chemical group 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- 238000001311 chemical methods and process Methods 0.000 description 1
- 239000010710 diesel engine oil Substances 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
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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
- C10G55/00—Treatment of hydrocarbon oils in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/06—Treatment of hydrocarbon oils in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one catalytic cracking step
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
Abstract
本发明是一种废矿物油催化裂解综合利用系统及其加工工艺，综合利用系统包括原料预处理系统、原料油预热系统、闪蒸催化裂解系统、溶剂精制系统、成品油储存系统、加热系统、残油后续加工处理系统和废水处理系统。加工工艺步骤分为原料预处理、原料油预热、闪蒸催化裂解和溶剂精制。本发明的加工工艺，既可以回收燃料油产品，又能够去除废矿物油中的杂质及水分，解决了废矿物油处理难的问题，整个过程中综合利用废水、废气，无废物排放，不存在环境污染问题，循环经济，节约能耗，应用前景广阔。本发明最后的精制油品，色泽澄清、透明，应用广泛。
Description
一种废矿物油催化裂解综合利用系统及其加工工艺
技术领域
[0001]本发明涉及废矿物油催化裂解综合利用的技术领域，尤其涉及一种废矿物油催化 裂解综合利用系统及其加工工艺。
背景技术
[0002]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 使用时被更换下来的油。废矿物油里含有金属肩末、灰尘、砂粒、纤维物质等杂质和水分。废 矿物油广泛产生并存在于工业生产的各个领域，如电厂每半年至两年换下大量的汽轮机 油、齿轮油;冶金行业排放失去功效的机械油、抗磨液压油;汽车修理厂每天换下的车辆齿 轮油和汽、柴油发动机油等。
[0003] 废矿物油，含有多种毒性，如果倒入土壤可致植物死亡，倒入水源，1吨废矿物油就 可污染100万吨饮用水。废矿物油成分复杂、数量大、危害性强，属于《国家危险废物名录》环 境保护部令第39号文所列“HW08废矿物油及含废矿物油废物”。
[0004]目前废矿物油的处理工艺主要有蒸馏-酸洗-白土精制工艺、沉降-酸洗-白土蒸馏 工艺、沉降-蒸馏-酸洗-钙土精制工艺、白土高温接触无酸再生工艺、蒸馏-乙醇抽提-白土 精制工艺、蒸馏-糠醛精制-白土精制工艺、沉降-絮凝-白土精制工艺等。上述工艺均存在产 生大量固废、酸渣等二次危废的缺点。
[0005]随着对废矿物油回收利用的深入研究以及对环保的要求越来越高，中国专利 CN105441122 A公开了一种废矿物油循环闪蒸催化裂解回收工艺，该技术方案中公开了废 矿物油回收处理的步骤包括:过滤沉淀、中间贮存、循环闪蒸、催化蒸馏、冷却回收。随着废 矿物油处理量的增大，固废-含油过滤网的产生量也会随着增加，含油过滤网的无害化处理 带来一定的困难。
[0006] 中国专利CN 105132011 A公开了废矿物油制备润滑油基础原料油的装置及其加 工工艺，其装置包括原料罐、再生罐、调和釜、过滤器以及成品罐，其工艺包括制备脱色剂、 搅拌混合、调和抽取、过滤、获得成品。本工艺方法会产生新的固废含油废脱色剂，且回收的 成品油纯度不高。
[0007] 中国专利CN 106350112 A公开了一种废矿物油预处理-加氢再生润滑油基础油的 方法，该技术方案废矿物油的预处理部分包括沉降脱水、水洗、碟片式离心机离心、卧式离 心机离心、刮膜蒸发器蒸发和减压蒸馏步骤，预处理后的润滑油基础油料再进入加氢装置， 先进入预加氢保护反应器，然后再进入加氢精制反应器，生产出高档次的润滑油基础油。该 工艺使用氢气精制，首先需要解决氢源，其次氢气作为易燃易爆气体，属于重点监管的危险 化工工艺，且生产成本较高。
发明内容
[0008] 本发明旨在解决现有技术的不足，而提供一种废矿物油催化裂解综合利用系统及 其加工工艺。
[0009] 本发明为实现上述目的，采用以下技术方案： 、
[0010] 一种废矿物油催化裂解综合利用系统，包括原料预处理系统、原料油预热系统、闪 蒸催化裂解系统、溶剂精制系统、成品油储存系统、加热系统、残油后续加工处理系统和废 水处理系统，原料预处理系统、原料油预热系统、闪蒸催化裂解系统和溶剂精制系统依次相 连，原料预处理系统分别与残油后续加工处理系统、废水处理系统相连，所述加热系统与原 料油预热系统、闪蒸催化裂解系统相连，原料油预热系统、闪蒸催化裂解系统、溶剂精制系 统均与成品油储存系统相连。 #
[0011] 所述原料预处理系统包括三格澄清罐、缓冲罐、原料油储罐、残油储罐和废水接收 罐，所述三格澄清罐顶层与所述缓冲罐相连，所述缓冲罐与所述原料油储罐相连，所述三格 澄清罐中层与所述废水接收罐相连，所述三格澄清罐底层与所述残油储罐相连；
[0012] 所述残油后续加工处理系统包括微波热解炉或碳化焚烧炉，所述残油储罐与所述 微波热解炉、碳化焚烧炉相连；
[0013] 所述废水处理系统包括废水收集池和废水处理装置，所述废水接收罐与所述废水 收集池相连，所述废水收集池与所述废水处理装置相连；
[0014] 所述原料油预热系统包括原料油预热罐、一级预热罐、汽包、减压罐和第一冷凝 器，所述原料油预热罐分别与所述原料油储罐、一级预热罐、汽包相连，所述一级预热罐与 汽包相连，所述汽包与所述减压罐相连，所述减压罐与所述第一冷凝器相连；
[0015] 所述闪蒸催化裂解系统包括闪蒸塔、催化塔、整理罐、裂解塔、换热器和第二冷凝 器，所述闪蒸塔与所述一级预热罐相连，所述闪蒸塔的塔顶和塔底分别和催化塔、裂解塔相 连，所述催化塔与所述整理罐相连，所述整理罐、裂解塔均与所述换热器相连，所述换热器 与第二冷凝器相连；
[0016] 所述溶剂精制系统包括萃取塔和溶剂回收塔，所述萃取塔与所述第二冷凝器相 连，所述萃取塔的萃取后溶剂出口与所述溶剂回收塔相连；
[0017] 所述成品油储存系统包括轻质燃油成品罐，所述轻质燃油成品罐分别与所述第一 冷凝器、第二冷凝器、萃取塔相连；
[0018] 所述加热系统包括水封罐、阻火器和加热炉，所述水封罐、阻火器和加热炉依次相 连，所述水封罐与第一冷凝器、第二冷凝器相连，所述加热炉与原料油预热罐、一级预热罐、 闪蒸塔、裂解塔相连。
[0019] 所述原料油预热罐与所述换热器之间设有循环管道。
[0020] 上述废矿物油催化裂解综合利用系统的加工工艺，具体步骤为：
[0021] a、原料预处理
[0022] 废矿物油进入二格澄清罐进彳丁分_，轻质油组分浮于最上层、中间层为废水、杂质 矿物油沉于最底层;轻质油组分溢流至缓冲罐，经栗提升至原料油储罐，底层杂质矿物油经 泵提升至残油储罐，随后进入微波热解炉或碳化焚烧炉进行后续加工处理，中间层废水经 废水接收罐收集进入废水收集池，经废水处理装置处理达标后作为循环水冷却水使用；
[0023] b、原料油预热
[0024] 澄清后的原料油从原料油储罐用泵送至原料油预热罐，与加热炉内的热油混合预 热至65_85°C，原料油预热罐挥发出的轻质组分通过汽包、减压罐进行减压，然后再进入第 一冷凝器冷却，最后进入轻质燃油成品罐储存；
[0025]原料油预热罐出来的部分原料油经循环管道进入换热器与催化塔或裂解塔出来 的物料进行换热之后，再经循环管道回到原料油预热罐，节约热能，实现预热；
[0026]原料油预热罐预热后的原料经油栗送入一级预热罐，与加热炉内的热油混合预热 至l5〇_2〇(TC，一级预热罐挥发出的轻质组分通过汽包、减压罐进行减压，然后再进入第一 冷凝器冷却，最后进入轻质燃油成品罐储存；
[0027] c、闪蒸催化裂解
[0028] —级预热罐中的原料油进入闪蒸塔，闪蒸塔内原料油经加热炉循环加热控制出口 温度在350-400°C，闪蒸塔塔顶的轻质组分进入催化塔加入催化剂进行催化改性，改性完成 后进入整理罐，经换热器和第二冷凝器冷却后，检测是否合格，若合格送至轻质燃油成品罐 储存，否则去萃取塔萃取；
[0029]闪蒸塔塔底的重质组分进入裂解塔发生碳链断裂，产生裂解汽油、柴油、燃料油， 经换热器和第二冷凝器冷却后，检测是否合格，若合格送至轻质燃油成品罐储存，否则去萃 取塔萃取；
[0030]第一冷凝器、第二冷凝器所产生的不凝气体进入水封罐经阻火器进入加热炉焚烧 加热原料油；
[0031] d、溶剂精制
[0032]经过闪蒸塔、催化塔和裂解塔催化裂解处理后回收的燃油进入萃取塔，进行溶剂 抽提，得到精制油品进入轻质燃油成品罐储存，萃取溶剂进入溶剂回收塔实现溶剂回收。 [0033]所述闪蒸塔、催化塔共有两个;所述加热炉共有五台，其中四台是使用状态，一台 为备用状态，所述加热炉为卧式盘管加热炉。
[0034]闪蒸塔塔顶的轻质组分进入催化塔加入催化剂进行催化改性过程中，催化剂采用 的是负载1%。氧化铝的ZSM-5分子筛。
[0035]溶剂精制过程采取单级或多级萃取，萃取的方式为逆流萃取或错流萃取。
[0036]溶剂精制过程中溶剂与燃油的质量比为2-50。
[0037]溶剂精制过程采用的萃取剂为糠醛、丙烷、N-甲基吡咯烷酮、DAA、四氢咲喃、甲醇 和环己酮中的一种或多种。
[0038]本发明的有益效果是:本发明的加工工艺，既可以回收燃料油产品，又能够去除废 矿物油中的杂质及水分，解决了废矿物油处理难的问题，整个过程中综合利用废水、废气， 无废物排放，不存在环境污染问题，循环经济，节约能耗，应用前景广阔。本发明最后的精制 油品，色泽澄清、透明，应用广泛。
附图说明
[0039]图1为本发明的具体设备连接示意图；
[0040]图2为本发明的系统结构示意图；
[0041]图中：卜三格澄清罐;2-缓冲罐;3-原料油储罐;4-残油储罐;5—废水接收罐;6_微 波热解炉;碳化焚烧炉;8-废水收集池;9-废水处理装置;10-原料油预热罐;11 级预热 罐；12-汽包；13-减压罐；14-第一冷凝器；15-闪蒸塔；16_催化塔；I7-整理罐；裂解塔. I9-换热器;2〇-第二冷凝器;21-萃取塔;22_溶剂回收塔;23_轻质燃油成品罐;24-水封罐； 25-阻火器;26-加热炉；
[0042]以下将结合本发明的实施例参照附图进行详细叙述。
具体实施方式
[0043]下面结合附图和实施例对本发明作进一步说明：
[0044] 具体实施例1:
[0045] 如图1和图2所示，一种废矿物油催化裂解综合利用系统，包括原料预处理系统、原 料油预热系统、闪蒸催化裂解系统、溶剂精制系统、成品油储存系统、加热系统、残油后续加 工处理系统和废水处理系统，原料预处理系统、原料油预热系统、闪蒸催化裂解系统和溶剂 精制系统依次相连，原料预处理系统分别与残油后续加工处理系统、废水处理系统相连，所 述加热系统与原料油预热系统、闪蒸催化裂解系统相连，原料油预热系统、闪蒸催化裂解系 统、溶剂精制系统均与成品油储存系统相连。
[0046] 所述原料预处理系统包括三格澄清罐1、缓冲罐2、原料油储罐3、残油储罐4和废水 接收罐5,所述三格澄清罐1顶层与所述缓冲罐2相连，所述缓冲罐2与所述原料油储罐3相 连，所述三格澄清罐1中层与所述废水接收罐5相连，所述三格澄清罐1底层与所述残油储罐 4相连；
[0047] 所述残油后续加工处理系统包括微波热解炉6或碳化焚烧炉7,所述残油储罐4与 所述微波热解炉6、碳化焚烧炉7相连；
[0048] 所述废水处理系统包括废水收集池8和废水处理装置9,所述废水接收罐5与所述 废水收集池8相连，所述废水收集池8与所述废水处理装置9相连；
[0049] 所述原料油预热系统包括原料油预热罐10、一级预热罐11、汽包12、减压罐13和第 一冷凝器14,所述原料油预热罐10分别与所述原料油储罐3、一级预热罐11、汽包12相连，所 述一级预热罐11与汽包12相连，所述汽包12与所述减压罐I3相连，所述减压罐13与所述第 一冷凝器14相连；
[0050] 所述闪蒸催化裂解系统包括闪蒸塔15、催化塔16、整理罐17、裂解塔18、换热器19 和第二冷凝器20,所述闪蒸塔15与所述一级预热罐11相连，所述闪蒸塔I5的塔顶和塔底分 别和催化塔16、裂解塔18相连，所述催化塔16与所述整理罐17相连，所述整理罐17、裂解塔 18均与所述换热器19相连，所述换热器19与第二冷凝器20相连；
[0051] 所述溶剂精制系统包括萃取塔21和溶剂回收塔22,所述萃取塔21与所述第二冷凝 器20相连，所述萃取塔21的萃取后溶剂出口与所述溶剂回收塔22相连；
[0052] 所述成品油储存系统包括轻质燃油成品罐23,所述轻质燃油成品罐23分别与所述 第一冷凝器14、第二冷凝器20、萃取塔21相连；
[0053] 所述加热系统包括水封罐24、阻火器25和加热炉26,所述水封罐24、阻火器25和加 热炉26依次相连，所述水封罐24与第一冷凝器14、第二冷凝器20相连，所述加热炉26与原料 油预热罐10、一级预热罐11、闪蒸塔15、裂解塔18相连。
[0054] 所述原料油预热罐10与所述换热器19之间设有循环管道。
[0055] 上述废矿物油催化裂解综合利用系统的加工工艺，具体步骤为：
[0056] a、原料预处理：
[0057]废矿物油进入三格澄清罐1进行分离，轻质油组分浮于最上层、中间层为废水、杂 质矿物油沉于最底层;轻质油组分溢流至缓冲罐2,经栗提升至原料油储罐3,底层杂质矿物 油经泵提升至残油储罐4,随后进入微波热解炉6或碳化焚烧炉7进行后续加工处理，中间层 废水经废水接收罐5收集进入废水收集池8，经废水处理装置9处理达标后作为循环水冷却 水使用；
[0058] b、原料油预热
[0059]澄清后的原料油从原料油储罐3用栗送至原料油预热罐10,与加热炉26内的热油 混合预热至65°C，原料油预热罐10挥发出的轻质组分通过汽包12、减压罐13进行减压，然后 再进入第一冷凝器14冷却，最后进入轻质燃油成品罐23储存； ‘
[0060]原料油预热罐10出来的部分原料油经循环管道进入换热器19与催化塔16或裂解 塔18出来的物料进行换热之后，再经循环管道回到原料油预热罐1〇,节约热能，实现预热； [0061]原料油预热罐10预热后的原料经油泵送入一级预热罐11，与加热炉26内的热油混 合预热至l5〇°C，一级预热罐11挥发出的轻质组分通过汽包12、减压罐13进行减压，然后再 进入第一冷凝器14冷却，最后进入轻质燃油成品罐23储存；
[0062] c、闪蒸催化裂解
[0063] 一级预热罐11中的原料油进入闪蒸塔15，闪蒸塔15内原料油经加热炉26循环加热 控制出口温度在350°C，闪蒸塔I5塔顶的轻质组分进入催化塔16加入催化剂进行催化改性， 改性完成后进入整理罐17,经换热器19和第二冷凝器20冷却后，检测是否合格，若合格送至 轻质燃油成品罐23储存，否则去萃取塔21萃取；
[0064]闪蒸塔15塔底的重质组分进入裂解塔发生碳链断裂，产生裂解汽油、柴油、燃料 油，经换热器19和第二冷凝器20冷却后，检测是否合格，若合格送至轻质燃油成品罐23储 存，否则去萃取塔21萃取；
[0065]检测合格的标准为中国石油化工总公司石油化工科学研究院起草、提出并归口的 石油化工行业标准《燃料油》(SH/T 0356-1996)。
[0066] 第一冷凝器14、第二冷凝器20所产生的不凝气体进入水封罐24经阻火器25进入加 热炉26焚烧加热原料油；
[0067] d、溶剂精制
[0068] 经过闪蒸塔15、催化塔16和裂解塔18催化裂解处理后回收的燃油进入萃取塔21， 进行溶剂抽提，得到精制油品进入轻质燃油成品罐23储存，萃取溶剂进入溶剂回收塔22实 现溶剂回收。
[0069] 所述闪蒸塔15、催化塔16共有两个;所述加热炉26共有五台，其中四台是使用状 态，一台为备用状态，所述加热炉26为卧式盘管加热炉。
[0070] 闪蒸塔15塔顶的轻质组分进入催化塔16加入催化剂进行催化改性过程中，催化剂 采用的是负载1%。氧化铝的ZSM-5分子筛。
[0071] 溶剂精制过程采取单级逆流萃取。
[0072] 溶剂精制过程中溶剂与燃油的质量比为2。
[0073] 溶剂精制过程采用的萃取剂为糠醛。
[0074] 具体实施例2:
[0075] 如图1和图2所示，一种废矿物油催化裂解综合利用系统，包括原料预处理系统、原 料油预热系统、闪蒸催化裂解系统、溶剂精制系统、成品油储存系统、加热系统、残油后续加 工处理系统和废水处理系统，原料预处理系统、原料油预热系统、闪蒸催化裂解系统和溶剂 精制系统依次相连，原料预处理系统分别与残油后续加工处理系统、废水处埋系轨彳日二尸乃 述加热系统与原料麵热系统、闪蒸催化裂解系统相连，原料油讎系统、闪蒸催化裂解系 统、溶剂精制系统均与成品油储存系统相连。
[0076] 所述原料预处理系统包括三格澄清罐1、缓冲罐2、原料油储罐3、残油储罐4和废水 接收罐5,所述三格澄清罐1顶层与所述缓冲罐2相连，所述缓冲罐2与所述原料油储罐3相 连，所述三格澄清罐1中层与所述废水接收罐5相连，所述三格澄清罐1底层与所述残油储罐 4相连； _
[0077] 所述残油后续加工处理系统包括微波热解炉6或碳化焚烧炉7,所述残油储罐4与 所述微波热解炉6、碳化焚烧炉7相连；
[0078] 所述废水处理系统包括废水收集池8和废水处理装置9,所述废水接收罐5与所述 废水收集池8相连，所述废水收集池8与所述废水处理装置9相连；
[0079] 所述原料油预热系统包括原料油预热罐1〇、一级预热罐11、汽包12、减压罐13和第 一冷凝器14,所述原料油预热罐10分别与所述原料油储罐3、一级预热罐11、汽包12相连，所 述一级预热罐11与汽包12相连，所述汽包12与所述减压罐13相连，所述减压罐13与所述第 一冷凝器14相连；
[0080] 所述闪蒸催化裂解系统包括闪蒸塔15、催化塔16、整理罐17、裂解塔18、换热器19 和第二冷凝器20,所述闪蒸塔15与所述一级预热罐11相连，所述闪蒸塔15的塔顶和塔底分 别和催化塔16、裂解塔18相连，所述催化塔16与所述整理罐I7相连，所述整理罐丨7、裂解塔 18均与所述换热器19相连，所述换热器19与第二冷凝器20相连；
[0081 ]所述溶剂精制系统包括萃取塔21和溶剂回收塔22，所述萃取塔21与所述第二冷凝 器20相连，所述萃取塔21的萃取后溶剂出口与所述溶剂回收塔22相连；
[0082] 所述成品油储存系统包括轻质燃油成品罐23,所述轻质燃油成品罐23分别与所述 第一冷凝器14、第二冷凝器20、萃取塔21相连；
[0083] 所述加热系统包括水封罐24、阻火器25和加热炉26,所述水封罐24、阻火器25和加 热炉26依次相连，所述水封罐24与第一冷凝器14、第二冷凝器20相连，所述加热炉26与原料 油预热罐10、一级预热罐11、闪蒸塔15、裂解塔18相连。
[0084] 所述原料油预热罐10与所述换热器19之间设有循环管道。
[0085] 上述废矿物油催化裂解综合利用系统的加工工艺，具体步骤为：
[0086] a、原料预处理：
[0087]废矿物油进入三格澄清罐1进行分离，轻质油组分浮于最上层、中间层为废水、杂 质矿物油沉于最底层;轻质油组分溢流至缓冲罐2,经栗提升至原料油储罐3,底层杂质矿物 油经栗提升至残油储罐4，随后进入微波热解炉6或碳化焚烧炉7进行后续加工处理，中间层 废水经废水接收罐5收集进入废水收集池8，经废水处理装置9处理达标后作为循环水冷却 水使用；
[0088] b、原料油预热
[0089]澄清后的原料油从原料油储罐3用泵送至原料油预热罐10,与加热炉26内的热油 混合预热至85°C，原料油预热罐10挥发出的轻质组分通过汽包12、减压罐13进行减压，然后 再进入第一冷凝器14冷却，最后进入轻质燃油成品罐23储存； _
[0090]原料油预热罐10出来的部分原料油经循环管道进入换热器IQ与催化塔16或裂解 塔18出来的物料进行换热之后，再经循环管道回到原料油预热罐1〇,节约热能，实现预热； [0091]原料油预热罐10预热后的原料经油栗送入一级预热罐11，与加热炉26内的热油混 合预热至200°C，一级预热罐11挥发出的轻质组分通过汽包12、减压罐13进行减压，然后再 进入第一冷凝器14冷却，最后进入轻质燃油成品罐23储存； ^
[0092] c、闪蒸催化裂解
[0093] 一级预热罐11中的原料油进入闪蒸塔15，闪蒸塔15内原料油经加热炉26循环加热 控制出口温度在40(TC，闪蒸塔15塔顶的轻质组分进入催化塔ie加入催化剂进行催化改性， 改性完成后进入整理罐I7,经换热器19和第二冷凝器2〇冷却后，检测是否合格，若合格送至 轻质燃油成品罐23储存，否则去萃取塔21萃取；
[0094]闪蒸塔15塔底的重质组分进入裂解塔发生碳链断裂，产生裂解汽油、柴油、燃料 油，经换热器19和第二冷凝器20冷却后，检测是否合格，若合格送至轻质燃油成品罐23储 存，否则去萃取塔21萃取；
[0095] 检测合格的标准为中国石油化工总公司石油化工科学研宄院起草、提出并归口的 石油化工行业标准《燃料油》(SH/T 0356-1996)。
[0096] 第一冷凝器14、第二冷凝器20所产生的不凝气体进入水封罐24经阻火器25进入加 热炉26焚烧加热原料油；
[0097] d、溶剂精制
[0098] 经过闪蒸塔15、催化塔16和裂解塔18催化裂解处理后回收的燃油进入萃取塔21， 进行溶剂抽提，得到精制油品进入轻质燃油成品罐23储存，萃取溶剂进入溶剂回收塔22实 现溶剂回收。
[0099] 所述闪蒸塔15、催化塔16共有两个;所述加热炉26共有五台，其中四台是使用状 态，一台为备用状态，所述加热炉26为卧式盘管加热炉。
[0100] 闪蒸塔15塔顶的轻质组分进入催化塔16加入催化剂进行催化改性过程中，催化剂 采用的是负载1%。氧化铝的ZSM-5分子筛。
[0101] 溶剂精制过程采取多级萃取错流萃取。
[0102] 溶剂精制过程中溶剂与燃油的质量比为50。
[0103] 溶剂精制过程采用的萃取剂为N-甲基吡咯烷酮。
[0104] 具体实施例3:
[0105] 如图1和图2所示，一种废矿物油催化裂解综合利用系统，包括原料预处理系统、原 料油预热系统、闪蒸催化裂解系统、溶剂精制系统、成品油储存系统、加热系统、残油后续加 工处理系统和废水处理系统，原料预处理系统、原料油预热系统、闪蒸催化裂解系统和溶剂 精制系统依次相连，原料预处理系统分别与残油后续加工处理系统、废水处理系统相连，所 述加热系统与原料油预热系统、闪蒸催化裂解系统相连，原料油预热系统、闪蒸催化裂解系 统、溶剂精制系统均与成品油储存系统相连。
[0106] 所述原料预处理系统包括三格澄清罐1、缓冲罐2、原料油储罐3、残油储罐4和废水 接收罐5,所述三格澄清罐1顶层与所述缓冲罐2相连，所述缓冲罐2与所述原料油储罐3才f 连，所述三格澄清罐1中层与所述废水接收罐5相连，所述三格澄清罐1底层与所述残油储罐 4相连； _
[0107] 所述残油后续加工处理系统包括微波热解炉6或碳化焚烧炉7,所述残油储罐4与 所述微波热解炉6、碳化焚烧炉7相连； > #
[0108] 所述废水处理系统包括废水收集池8和废水处理装置9,所述废水接收罐5与所述 废水收集池8相连，所述废水收集池8与所述废水处理装置9相连；
[0109] 所述原料油预热系统包括原料油预热罐1〇、一级预热罐11、汽包12、减压罐13和第 一冷凝器14,所述原料油预热罐1〇分别与所述原料油储罐3、一级预热罐n、汽包12相连，所 述一级预热罐11与汽包12相连，所述汽包12与所述减压罐13相连，所述减压罐13与所述第 一冷凝器14相连；
[0110] 所述闪蒸催化裂解系统包括闪蒸塔15、催化塔16、整理罐I7、裂解塔18、换热器19 和第二冷凝器20，所述闪蒸塔15与所述一级预热罐11相连，所述闪蒸塔15的塔顶和塔底分 别和催化塔16、裂解塔18相连，所述催化塔16与所述整理罐17相连，所述整理罐17、裂解塔 18均与所述换热器19相连，所述换热器19与第二冷凝器20相连；
[0111] 所述溶剂精制系统包括萃取塔21和溶剂回收塔，所述萃取塔21与所述第二冷凝 器20相连，所述萃取塔21的萃取后溶剂出口与所述溶剂回收塔22相连；
[0112] 所述成品油储存系统包括轻质燃油成品罐23,所述轻质燃油成品罐23分别与所述 第一冷凝器14、第二冷凝器20、萃取塔21相连；
[0113] 所述加热系统包括水封罐24、阻火器25和加热炉26,所述水封罐24、阻火器25和加 热炉26依次相连，所述水封罐24与第一冷凝器14、第二冷凝器20相连，所述加热炉26与原料 油预热罐10、一级预热罐11、闪蒸塔15、裂解塔18相连。
[0114] 所述原料油预热罐10与所述换热器19之间设有循环管道。
[0115] 上述废矿物油催化裂解综合利用系统的加工工艺，具体步骤为：
[0116] a、原料预处理：
[0117] 废矿物油进入三格澄清罐1进行分离，轻质油组分浮于最上层、中间层为废水、杂 质矿物油沉于最底层;轻质油组分溢流至缓冲罐2,经泵提升至原料油储罐3,底层杂质矿物 油经泵提升至残油储罐4，随后进入微波热解炉6或碳化焚烧炉7进行后续加工处理，中间层 废水经废水接收罐5收集进入废水收集池8，经废水处理装置9处理达标后作为循环水冷却 水使用；
[0118] b、原料油预热
[0119]澄清后的原料油从原料油储罐3用泵送至原料油预热罐1〇,与加热炉26内的热油 混合预热至70°C，原料油预热罐10挥发出的轻质组分通过汽包12、减压罐13进行减压，然后 再进入第一冷凝器14冷却，最后进入轻质燃油成品罐23储存； ^
[0120]原料油预热罐10出来的部分原料油经循环管道进入换热器19与催化塔16或裂解 塔1S出来的物料进行换热之后，再经循环管道回到原料油预热罐1〇,节约热能，实现^热； [0121]原料油预热罐10预热后的原料经油栗送入一级预热罐11，与加热炉26内的热油混 合预热至18(TC，一级预热罐11挥发出的轻质组分通过汽包12、减压罐13‘进行减压，^后再 进入第一冷凝器14冷却，最后进入轻质燃油成品罐23储存； ^
[0122] c、闪蒸催化裂解
[0123] —级预热罐11中的原料油进入闪蒸塔15,闪蒸塔15内原料油经加热炉26循环加热 控制出口温度在37(TC，闪蒸塔15塔顶的轻质组分进入催化塔16加入催化剂进行催化改性'，' 改性完成后进入整理罐17,经换热器19和第二冷凝器20冷却后,检测是否合格，若合格送至 轻质燃油成品罐23储存，否则去萃取塔21萃取；
[0124] 闪蒸塔15塔底的重质组分进入裂解塔发生碳链断裂，产生裂解汽油、柴油、燃料 油，经换热器19和第二冷凝器20冷却后，检测是否合格，若合格送至轻质燃油成品罐23储 存，否则去萃取塔21萃取；
[0125] 检测合格的标准为中国石油化工总公司石油化工科学研宄院起草、提出并归口的 石油化工行业标准《燃料油》(SH/T 0356-1996)。
[0126] 第一冷凝器14、第二冷凝器20所产生的不凝气体进入水封罐24经阻火器25进入加 热炉26焚烧加热原料油；
[0127] d、溶剂精制
[0128] 经过闪蒸塔15、催化塔16和裂解塔18催化裂解处理后回收的燃油进入萃取塔21， 进行溶剂抽提，得到精制油品进入轻质燃油成品罐23储存，萃取溶剂进入溶剂回收塔22实 现溶剂回收。
[0129] 所述闪蒸塔15、催化塔16共有两个;所述加热炉26共有五台，其中四台是使用状 态，一台为备用状态，所述加热炉26为卧式盘管加热炉。
[0130]闪蒸塔I5塔顶的轻质组分进入催化塔16加入催化剂进行催化改性过程中，催化剂 采用的是负载1%。氧化铝的ZSM-5分子筛。
[0131] 溶剂精制过程采取单级错流萃取。
[0132] 溶剂精制过程中溶剂与燃油的质量比为25。
[0133] 溶剂精制过程采用的萃取剂为四氢呋喃。
[0134]本发明的加工工艺，既可以回收燃料油产品，又能够去除废矿物油中的杂质及水 分，解决了废矿物油处理难的问题，整个过程中综合利用废水、废气，无废物排放，不存在环 境污染问题，循环经济，节约能耗，应用前景广阔。本发明最后的精制油品，闪点为90-100 °C，密度为0.84-0.88g/cm3,色泽澄清、透明，应用广泛。
[0135]上面结合附图对本发明进行了示例性描述，显然本发明具体实现并不受上述方式 的限制，只要采用了本发明的方法构思和技术方案进行的各种改进，或未经改进直接应用 于其它场合的，均在本发明的保护范围之内。
Claims (9)
1. 一种废矿物油催化裂解综合利用系统，包括原料预处理系统、原料油预热系统、闪蒸 催化裂解系统、溶剂精制系统、成品油储存系统、加热系统、残油后续加工处理系统和废水 处理系统，其特征在于，原料预处理系统、原料油预热系统、闪蒸催化裂解系统和溶剂精制 系统依次相连，原料预处理系统分别与残油后续加工处理系统、废水处理系统相连，所述加 热系统与原料油预热系统、闪蒸催化裂解系统相连，原料油预热系统、闪蒸催化裂解系统、 溶剂精制系统均与成品油储存系统相连。
2. 根据权利要求1所述的一种废矿物油催化裂解综合利用系统，其特征在于，所述原料 预处理系统包括三格澄清罐（1)、缓冲罐(2)、原料油储罐(3)、残油储罐⑷和废水接收罐 (5)，所述三格澄清罐(1)顶层与所述缓冲罐相连，所述缓冲罐⑵与所述原料油储罐(3) 相连，所述三格澄清罐(1)中层与所述废水接收罐(5)相连，所述三格澄清罐⑴底层与所述 残油储罐⑷相连； 所述残油后续加工处理系统包括微波热解炉(6)或碳化焚烧炉(7)，所述残油储罐(4) 与所述微波热解炉(6)、碳化焚烧炉(7)相连； 所述废水处理系统包括废水收集池(8)和废水处理装置(9)，所述废水接收罐(5)与所 述废水收集池(8)相连，所述废水收集池(8)与所述废水处理装置(9)相连； 所述原料油预热系统包括原料油预热罐（10)、一级预热罐(11)、汽包（12)、减压罐(13) 和第一冷凝器（14)，所述原料油预热罐（10)分别与所述原料油储罐(3)、一级预热罐（11)、 汽包（12)相连，所述一级预热罐（11)与汽包（12)相连，所述汽包（12)与所述减压罐（13)相 连，所述减压罐(13)与所述第一冷凝器(14)相连； 所述闪蒸催化裂解系统包括闪蒸塔（15)、催化塔（16)、整理罐（17)、裂解塔（18)、换热 器（19)和第二冷凝器(20)，所述闪蒸塔（15)与所述一级预热罐（11)相连，所述闪蒸塔(15) 的塔顶和塔底分别和催化塔（16)、裂解塔（18)相连，所述催化塔（16)与所述整理罐（17)相 连，所述整理罐(17)、裂解塔(18)均与所述换热器(19)相连，所述换热器(19)与第二冷凝器 (20)相连； 所述溶剂精制系统包括萃取塔(21)和溶剂回收塔(22)，所述萃取塔(21)与所述第二冷 凝器(20)相连，所述萃取塔(21)的萃取后溶剂出口与所述溶剂回收塔(22)相连； 所述成品油储存系统包括轻质燃油成品罐(23)，所述轻质燃油成品罐(23)分别与所述 第一冷凝器(14)、第二冷凝器(20)、萃取塔(21)相连； 所述加热系统包括水封罐（24)、阻火器(25)和加热炉（26)，所述水封罐（24)、阻火器 (25)和加热炉(26)依次相连，所述水封罐(24)与第一冷凝器(14)、第二冷凝器(20)相连，所 述加热炉(26)与原料油预热罐(10)、一级预热罐(11)、闪蒸塔(15)、裂解塔(18)相连。
3.根据权利要求2所述的一种废矿物油催化裂解综合利用系统，其特征在于，所述原料 油预热罐(10)与所述换热器(19)之间设有循环管道。
4.一种如权利要求3所述的废矿物油催化裂解综合利用系统的加工工艺，其特征在于， 具体步骤为： a、原料预处理 废矿物油进入三格澄清罐（1)进行分离，轻质油组分浮于最上层、中间层为废水、杂质 矿物油沉于最底层;轻质油组分溢流至缓冲罐(2)，经栗提升至原料油储罐(3)，底层杂质矿 物油经泵提升至残油储罐(4)，随后进入微波热解炉(6)或碳化焚烧炉(7)进行后续加工处 ^，中间层废水经废水接收罐⑸收集进入废水收集池⑻，经废水处理装置⑼处达标 作为循环水冷却水使用； b、 原料油预热 、、澄清后的原料油从原料油储罐⑶用泵送至原料油预热罐⑽，与加热炉⑽内的热 /油混合预热至65_85=，願油職罐⑽撤出陳讎分删：汽包⑽、减压罐⑽进 t丁减压，然后碰A第-騎器(M)冷却，最后进人轻质顯成罐(23)储存； 原料油预热罐do)出来的部分原料油经循环管道进入换热器（19)与催化塔（16)或裂 解塔⑽出来的物料进行换热之后，再经循环管道圆原料麵讎⑽，节约热能，实现 预热； 、原料油预热罐（10)预热后的原料经油泵送入一级预热罐(11)，与加热炉(26)内的热油 混合预热至150-200°C，一级预热罐（丨〖)挥发出的轻质组分通过汽包（12)、减压罐（13)进行 减压，然后再进入第一冷凝器(14)冷却，最后进入轻质燃油成品罐(23)储存； c、 闪蒸催化裂解 一级预热罐（11)中的原料油进入闪蒸塔（15)，闪蒸塔(15)内原料油经加热炉(26)循环 加^控制出口温度在35〇-400°C，闪蒸塔（u)塔顶的轻质组分进入催化塔（16)加入催化剂 进行催化改性，改性完成后进入整理罐（17)，经换热器（19)和第二冷凝器(20)冷却后，检测 是否合格，若合格送至轻质燃油成品罐(23)储存，否则去萃取塔(21)萃取； 闪蒸塔（15)塔底的重质组分进入裂解塔发生碳链断裂，产生裂解汽油、柴油、燃料油， 经换热器（19)和第二冷凝器(20)冷却后，检测是否合格，若合格送至轻质燃油成品罐(23) 储存，否则去萃取塔(21)萃取； 第一冷凝器（14)、第二冷凝器(2〇)所产生的不凝气体进入水封罐(24)经阻火器(25)进 入加热炉(26)焚烧加热原料油； d、 溶剂精制 经过闪蒸塔（15)、催化塔（16)和裂解塔（18)催化裂解处理后回收的燃油进入萃取塔 (21)，进行溶剂抽提，得到精制油品进入轻质燃油成品罐(23)储存，萃取溶剂进入溶剂回收 塔(22)实现溶剂回收。
5. 根据权利要求4所述的一种废矿物油催化裂解综合利用系统的加工工艺，其特征在 于，所述闪蒸塔（15)、催化塔（16)共有两个;所述加热炉（26)共有五台，其中四台是使用状 态，一台为备用状态，所述加热炉(26)为卧式盘管加热炉。
6. 根据权利要求5所述的一种废矿物油催化裂解综合利用系统的加工工艺，其特征在 于，闪蒸塔（15)塔顶的轻质组分进入催化塔（16)加入催化剂进行催化改性过程中，催化剂 采用的是负载1%。氧化铝的ZSM-5分子筛。
7. 根据权利要求6所述的一种废矿物油催化裂解综合利用系统的加工工艺，其特征在 于，溶剂精制过程采取单级或多级萃取，萃取的方式为逆流萃取或错流萃取。
8. 根据权利要求7所述的一种废矿物油催化裂解综合利用系统的加工工艺，其特征在 于，溶剂精制过程中溶剂与燃油的质量比为2-50。
9. 根据权利要求8所述的一种废矿物油催化裂解综合利用系统的加工工艺，其特征在 于，溶剂精制过程采用的萃取剂为糠醛、丙烷、N-甲基吡咯烷酮、DAA、四氢呋喃、甲醇和环己 酮中的一种或多种。
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| CN111718747A (zh) * | 2020-06-28 | 2020-09-29 | 海南绿新新能源有限公司 | 一种利用矿物油尾料生产低硫高值燃料油工艺方法 |
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| CN108395903A (zh) * | 2018-04-23 | 2018-08-14 | 张荣江 | 一种环保型废油塔管式逆流法辐射加热免酸萃取油工艺 |
| CN111718747A (zh) * | 2020-06-28 | 2020-09-29 | 海南绿新新能源有限公司 | 一种利用矿物油尾料生产低硫高值燃料油工艺方法 |
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