CN104740894B - 煤液化残渣的萃取系统与萃取方法 - Google Patents
煤液化残渣的萃取系统与萃取方法 Download PDFInfo
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- CN104740894B CN104740894B CN201510179149.5A CN201510179149A CN104740894B CN 104740894 B CN104740894 B CN 104740894B CN 201510179149 A CN201510179149 A CN 201510179149A CN 104740894 B CN104740894 B CN 104740894B
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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 144
- 239000003245 coal Substances 0.000 title claims abstract description 140
- 238000000034 method Methods 0.000 title claims abstract description 56
- CURLTUGMZLYLDI-UHFFFAOYSA-N carbon dioxide Chemical compound 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O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 126
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 124
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 124
- 238000000605 extraction Methods 0.000 claims abstract description 92
- 239000007788 liquid Substances 0.000 claims abstract description 74
- 239000000284 extract Substances 0.000 claims abstract description 50
- 238000004821 distillation Methods 0.000 claims description 20
- 239000000203 mixture Substances 0.000 claims description 19
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- 239000002245 particle Substances 0.000 claims description 10
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[C+4].[O-2].[O-2].[Ti+4] GCNLQHANGFOQKY-UHFFFAOYSA-N 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 239000000295 fuel oil Substances 0.000 description 3
- 238000005984 hydrogenation reaction Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- 229910002090 carbon oxide Inorganic materials 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titan oxide Chemical compound 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O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 241000790917 Dioxys <bee> Species 0.000 description 1
- DAAJPHTURITNKZ-UHFFFAOYSA-N [O-2].[O-2].[Ti+4].C(=O)=O Chemical compound 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Abstract
本发明提供了一种煤液化残渣的萃取系统与萃取方法。该萃取系统包括超临界二氧化碳发生单元以及与超临界二氧化碳发生单元连通的萃取单元。该萃取系统首先利用超临界二氧化碳发生单元产生超临界二氧化碳流体，其次，采用超临界二氧化碳流体对在萃取单元中的煤液化残渣进行萃取。超临界二氧化碳流体的扩散能力是普通液体的100倍，因而具有很好的溶解能力，它能够迅速渗透进入微孔隙的物质，进而实现对煤液化残渣中重质液化油的快速、高效地萃取分离。该方法只利用超临界二氧化碳发生单元与萃取单元就可以将重质液化油从煤液化残渣中萃取出来，工艺流程简单，克服了现有技术中萃取煤液化残渣工艺流程复杂的问题。
Description
煤液化残渣的萃取系统与萃取方法
技术领域
[0001] 本发明涉及煤炭化学加工领域，具体而言，涉及一种煤液化残渣的萃取系统与萃 取方法。
背景技术
[0002] 煤液化残渣是煤炭直接液化过程中的副产物，主要由重质液化油、沥青类物质、未 转化的煤、煤中的矿物质与外加的催化剂组成。重质液化油和沥青类物质约占残渣总量的 50%，未转化煤约占残渣总量的30%，灰分占20%左右。因此，可以将液化残渣中约占50% 的沥青类物质和重质液化油分离出来进行综合开发利用，从中提取出更有价值的产品，尤 其是将煤液化残渣中的重质液化油提取出来用作煤直接液化的循环溶剂，以提高整个煤直 接液化的收益。
[0003] 目前，煤液化残渣中重质液化油的提取多采用溶剂萃取的方法，如专利公开号为 CN101962560A与CN101962561A中国专利申请文件均公开了采用两级萃取法从煤液化残渣 中提取重质液化油和沥青类物质，该方法分别以煤直接液化过程自身产生的两个不同馏分 段的油品为萃取溶剂，对液化残渣进行两级顺序萃取，得到重质液化油与沥青类物质。
[0004] 上述方法虽然能得到重质液化油与沥青类物质，但是该方法需要进行两级萃取与 两次两级固液分离，工艺流程较复杂，成本较高;整个萃取过程用到较多的有机溶剂，对人 体的健康造成危害。
[0005] 针对上述问题，需要一种工艺流程较简单的煤液化残渣的萃取系统与萃取方法。
发明内容
[0006] 本发明的主要目的在于提供一种煤液化残渣的萃取系统与萃取方法，以解决现有 技术中煤液化残渣的萃取工艺流程较复杂的问题。
[0007] 为了实现上述目的，根据本发明的一个方面，提供了一种煤液化残渣的萃取系统， 上述萃取系统包括超临界二氧化碳发生单元以及与上述超临界二氧化碳发生单元连通的 萃取单元。
[0008] 进一步地，上述超临界二氧化碳发生单元包括：二氧化碳冷凝器、第一高压栗、混 合器与加热器，二氧化碳冷凝器将二氧化碳冷凝至超临界温度;第一高压栗与上述二氧化 碳冷凝器连通，将来自上述二氧化碳冷凝器的上述二氧化碳加压至超临界压力；混合器与 上述二氧化碳冷凝器连通，将夹带剂和上述二氧化碳混合形成混合物；加热器与上述混合 器和上述萃取单元连通，加热来自上述混合器的混合物。
[0009] 进一步地，上述超临界二氧化碳发生单元还包括第二高压栗，上述第二高压栗与 上述混合器连通将上述夹带剂栗入上述混合器中。
[0010] 进一步地，上述萃取系统还包括萃取物分离单元，上述萃取物分离单元与上述萃 取单元连通。
[0011] 进一步地，上述萃取物分离单元包括:分离釜与蒸馏釜，分离釜与上述萃取单元连 通，具有二氧化碳出口和液体出口；蒸馏釜与上述分离釜的液体出口连通，具有夹带剂出 □ 〇
[0012] 进一步地，上述分离爸通过上述二氧化碳出口与上述二氧化碳冷凝器连通。
[0013] 为了实现上述目的，根据本发明的另一个方面，提供了一种煤液化残渣的萃取方 法，上述萃取方法包括:对煤液化残渣进行二氧化碳超临界萃取，得到含有上述煤液化残渣 中的重质液化油的萃取液。
[0014] 进一步地，上述二氧化碳超临界萃取在夹带剂存在下进行。
[0015] 进一步地，上述夹带剂为正已烷和/或煤液化轻油。
[0016] 进一步地，上述夹带剂与超临界状态的二氧化碳的重量比为10:100〜40:100。
[0017] 进一步地，上述超临界萃取的温度在40〜80°C之间，优选上述超临界萃取的压力 在30〜45MPa之间。
[0018] 进一步地，上述煤液化残渣为粒径在0.2mm〜Imm之间的煤液化残渣粒子。
[0019] 进一步地，上述萃取方法在完成上述超临界萃取后还包括:步骤A，对上述萃取液 进行分离，得到分离的混合液和上述二氧化碳；以及步骤B，对上述混合液进行蒸馏，得到分 离的上述夹带剂和上述重质液化油。
[0020] 进一步地，上述分离的温度在30〜60°C之间，优选上述分离的压力在3〜6MPa之 间。
[0021] 进一步地，上述蒸馏为常压蒸馏或减压蒸馏。
[0022] 进一步地，上述步骤A得到的上述二氧化碳和上述步骤B得到的上述夹带剂可以返 回上述超临界萃取过程循环使用。
[0023] 应用本发明的技术方案，萃取系统首先利用超临界二氧化碳发生单元产生超临界 二氧化碳流体，其次采用超临界二氧化碳流体对在萃取单元中的煤液化残渣进行萃取，超 临界二氧化碳流体的扩散能力是普通液体的100倍，因而具有很好的溶解能力，它能够迅速 渗透进入微孔隙的物质，进而实现对煤液化残渣中重质液化油的快速、高效地萃取分离。该 方法只利用超临界二氧化碳发生单元与萃取单元就可以将重质液化油从煤液化残渣中萃 取出来，工艺流程简单，克服了现有技术中萃取煤液化残渣工艺流程复杂的问题。
附图说明
[0024] 构成本申请的一部分的说明书附图用来提供对本发明的进一步理解，本发明的示 意性实施例及其说明用于解释本发明，并不构成对本发明的不当限定。在附图中：
[0025] 图1示出了根据本发明的一种典型实施例的萃取系统的示意图；以及
[0026] 图2示出一种优选实施例的萃取方法工艺流程图。
具体实施方式
[0027] 需要说明的是，在不冲突的情况下，本申请中的实施例及实施例中的特征可以相 互组合。下面将参考附图并结合实施例来详细说明本发明。
[0028] 在本申请一种典型的实施方式中，提供了一种煤液化残渣的萃取系统，如图1所 示，上述萃取系统包括超临界二氧化碳发生单元10以及与上述超临界二氧化碳发生单元10 连通的萃取单元20。
[0029] 上述的萃取系统首先利用超临界二氧化碳发生单元10产生超临界二氧化碳流体， 其次，采用超临界二氧化碳流体对在萃取单元20中的煤液化进行萃取，超临界二氧化碳流 体的扩散能力是普通液体的100倍，因而具有很好的溶解能力，它能够迅速渗透进入微孔隙 的物质，进而实现对煤液化残渣中重质液化油的快速、高效地萃取分离。该方法只利用超临 界二氧化碳发生单元1与萃取单元2就可以将重质液化油从煤液化残渣中萃取出来，工艺流 程简单，克服了现有技术中萃取煤液化残渣工艺流程复杂的问题。
[0030] 为了进一步获得较稳定的超临界二氧化碳流体，进而利用其进行高效萃取，从煤 液化残渣中萃取出更多的重质液化油，提高萃取重质液化油的萃取率，如图2所示，本申请 优选上述超临界二氧化碳发生单元10包括二氧化碳冷凝器11、第一高压栗12、混合器13与 加热器14,二氧化碳冷凝器11将二氧化碳冷凝至超临界温度;第一高压栗12与上述二氧化 碳冷凝器11连通，将来自上述二氧化碳冷凝器11的上述二氧化碳加压至超临界压力；混合 器13与上述二氧化碳冷凝器11连通，将夹带剂和上述二氧化碳混合形成混合物；与上述二 氧化碳冷凝器11连通，将夹带剂和上述二氧化碳混合形成混合物;加热器14与上述混合器 13和上述萃取单元20连通，加热来自上述混合器的混合物。
[0031] 本申请又一种优选的实施例中，优选上述超临界二氧化碳发生单元10还包括第二 高压栗15,如图2所示，上述第二高压栗15与上述混合器13连通将上述夹带剂栗入上述混合 器13中。第二高压栗70中的压力较大，将夹带剂通入第二高压栗15,可以使得夹带剂的压力 进一步降低，避免夹带剂与超临界二氧化碳流体混合时将使超临界二氧化碳流体的温度升 高，进而避免使超临界二氧化碳流体变为气体，进而能够使超临界二氧化碳流体更稳定地 保持在超临界状态，进一步保证了后续萃取过程的顺利进行。
[0032] 为了方便材料的利用，进一步将重质液化油从萃取得到的超临界二氧化碳流体、 夹带剂与重质液化油组成的混合液中分离出来，同时将夹带剂与二氧化碳分离出来以进行 重复利用，本申请优选上述萃取物分离单元30包括分离釜31和蒸馏釜32,如图2所示，分离 釜31与上述萃取单元20连通，具有二氧化碳出口和液体出口；蒸馏釜32与上述分离釜31的 液体出口连通，具有夹带剂出口。
[0033] 本申请又一种优选的实施例中，如图2所示，优选上述分离釜31通过上述二氧化碳 出口与上述二氧化碳冷凝器11连通，这样最后分离出来的二氧化碳可以再次进入二氧化碳 冷凝器11，实现二氧化碳的循环利用，降低萃取成本，节约环保。
[0034] 为了使蒸馏釜32得到的夹带剂可以循环使用，降低萃取成本，提高夹带剂的利用 率，本申请优选上述蒸馏釜32通过上述夹带剂出口与上述混合器13连通。
[0035] 在本申请的又一种典型的实施方式中，提供了一种煤液化残渣的萃取方法，该萃 取方法包括:对煤液化残渣进行二氧化碳超临界萃取，得到含有上述煤液化残渣中的重质 液化油的萃取液。
[0036] 上述萃取方法利用上述萃取系统，与现有技术相比，该方法只利用超临界二氧化 碳流体就可以对煤液化残渣进行萃取，得到重质液化油，克服了现有萃取方法的工艺流程 较复杂的问题。
[0037] 由于重质液化油中的化合物的极性较大，在超临界二氧化碳流体中的溶解度较 小，为了提高重质液化油在超临界二氧化碳流体中的溶解度，使得极性较大的化合物更多 地溶解在二氧化碳与夹带剂的混合溶液中，进而从煤液化残渣中萃取出更多的重质液化 油，提高萃取效率。本申请优选上述二氧化碳超临界萃取在夹带剂存在下进行。
[0038] 根据煤液化残渣中重质液化油的组成特点，优选上述夹带剂为正已烷和/或煤液 化轻油。
[0039] 在本申请的一种优选的实施例中，上述夹带剂与上述超临界状态的二氧化碳的重 量比为10:100〜40:100。当夹带剂与超临界状态的二层氧化碳的重量比在10:100〜40:100 之间时，夹带剂可以较大程度地提高极性较大化合物的溶解度，使得极性较大的化合物更 多地溶解在二氧化碳与夹带剂的混合溶液中，进而可以从煤液化残渣中萃取出更多的重质 液化油，可以进一步提尚萃取率，提尚重质液化油的广率。
[0040] 二氧化碳的临界温度31.26°C，临界压力为7.386MPa，为了达到更好的重质液化油 萃取效果，优选超临界萃取的压力在30〜45MPa之间，因为重质液化油的极性较大，在超临 界二氧化碳流体中的溶解度较小，增加萃取压力增加重质液化油在超临界二氧化碳流体中 的溶解度，进一步增加重质液化油的萃取率。
[0041] 本申请的一种优选的实施例中，优选萃取温度在40〜80°C之间。萃取温度在40〜 80°C之间时，可以提高重质液化油在夹带剂和二氧化碳中的溶解度，进一步提高重质液化 油的萃取率。
[0042] 为了使煤液化残渣充分地与夹带剂和超临界二氧化碳流体的混合液接触，进一步 提高重质液化油的在其中的溶解度，本申请优选上述煤液化残渣为粒径在0.2mm〜Imm之间 的煤液化残渣粒子。
[0043] 本申请的又一种优选的实施例中，优选上述萃取方法在完成上述超临界萃取后还 包括:步骤A，对上述萃取液进行分离，得到分离的混合液和上述二氧化碳;步骤B，对上述混 合液进行蒸馏，得到分离的上述夹带剂和上述重质液化油。上述超临界萃取得到的萃取液 为超临界二氧化碳流体、夹带剂与重质液化油组成的混合液，对萃取液进行减压分离，二氧 化碳由超临界流体状态变为气体，实现气液分离，即二氧化碳从萃取液中分离出来，分离后 的混合液中的主要成分为夹带剂与重质液化油，对分离后的混合液进行蒸馏，利用夹带剂 与重质液化油的沸点的不同，将二者分离开来。这样将萃取液中的所有成分分离出来，方便 各成分的再次利用。
[0044] 为了进一步将萃取液中的所有超临界二氧化碳流体转变为气体，使二氧化碳与包 含夹带剂和重质液化油的混合液分离彻底，优选上述分离的温度在30〜60°C之间。
[0045] 进一步优选上述分离的压力在3〜6MPa之间。3〜6MPa的分离压力进一步保证了萃 取液中的超临界流体二氧化碳全部转化为气体，与夹带剂和重质液化油组成的混合液分离 开来。为了避免压力的骤降对萃取设备中的管道产生不良影响，在实际的工艺流程中，会设 置两个分离爸，分别为第一分离爸与第二分离爸，第一分离爸先将压力降低至9〜12MPa，将 一部分的二氧化碳分离出来，分离后的混合液再进入第二分离釜，将剩余的二氧化碳分离 出来。能够实现上述夹带剂和重质液化油的蒸馏方法和蒸馏条件有多种，考虑到操作的简 便性和安全性，优选上述蒸馏为常压蒸馏或减压蒸馏。
[0046] 为了使二氧化碳和夹带剂可以在超临界萃取过程中循环使用，降低超临界萃取的 成本，实现节约环保，本申请优选上述步骤A得到的上述二氧化碳和上述步骤B得到的上述 夹带剂可以返回上述超临界萃取过程循环使用。
[0047] 为了使本领域技术人员能够更加清楚地了解本申请的技术方案，以下将结合实施 例与对比例对本申请的技术方案进行详细说明。
[0048] 实施例1
[0049] 萃取的具体的工艺条件见表1所示。采用图2所示的萃取系统进行煤液化残渣的萃 取，取粒径为0.2〜I. Omm的煤液化残渣粒子500Kg，放入萃取单元20内并密封。控制二氧化 碳供应单元01中的二氧化碳以20L/h的流量经二氧化碳冷凝器11、第一高压栗12进入加热 器14,加热器14加热来自上述混合器13的混合物进一步保证二氧化碳为超临界状态。
[0050] 将加热器14中的二氧化碳送入萃取单元20中，萃取单元20内的压力为30MPa，温度 为60°C，在萃取单元20内对煤液化残渣进行萃取，得到萃取液，萃取液为包含超临界二氧化 碳流体与重质液化油的混合液。
[0051] 萃取液进入萃取物分离单元30的分离釜31中，分离釜31中的温度50°C，压力为 4MPa，在分离釜31中，二氧化碳由超临界流体状态转变为气体，从萃取液中分离出来，分离 出来的二氧化碳经二氧化碳出口再次进入二氧化碳冷凝器11中，实现循环利用。整个过程 持续运行3小时后，得到液化重油5Kg。
[0052] 实施例2
[0053] 萃取的具体的工艺条件见表1所示。采用图2所示的萃取系统进行煤液化残渣的萃 取，取粒径为1.2〜2. Omm的煤液化残渣粒子500Kg，放入萃取单元20内并密封。控制正己烷 与二氧化碳的重量比为10:100,二氧化碳经二氧化碳冷凝器11、第一高压栗12进入混合器 13,同时夹带剂供应单元03中的正己烷进入第二高压栗15中加压，然后第二高压栗15将作 为夹带剂的正已烷加入混合器13中。加热器14加热来自上述混合器13的混合物进一步保证 二氧化碳为超临界状态。
[0054] 将加热器14中的重量比为10:100的正己烷与二氧化碳送入萃取单元20中，萃取单 元20内的压力为30MPa，温度为60°C，在萃取单元20内对煤液化残渣进行萃取，得到萃取液， 萃取液为包含超临界二氧化碳流体、夹带剂与重质液化油的混合液。
[0055] 萃取液进入萃取物分离单元30的分离釜31中，分离釜31中的温度50°C，压力为 4MPa，在分离釜31中，二氧化碳有超临界流体状态转变为气体，从萃取液中分离出来，分离 出来的二氧化碳经二氧化碳出口再次进入二氧化碳供应单元〇 1中，实现循环利用。分离后 的混合液经过液体出口进入蒸馏釜32中，此时的混合液包括夹带剂与重质液化油，通过常 温蒸馏将夹带剂与重质液化油相继分离出来，如表2所示，整个过程持续运行3小时后，得到 液化重油30Kg。夹带剂经过夹带剂出口进入夹带剂供应单元03中，实现循环利用。
[0056] 实施例3
[0057] 萃取的具体的工艺条件见表1所示。采用图2所示的萃取系统进行煤液化残渣的萃 取，得到的重质液化油的重量与萃取率如表2所示。
[0058] 实施例4
[0059] 萃取的具体的工艺条件见表1所示。采用图2所示的萃取系统进行煤液化残渣的萃 取，得到的重质液化油的重量与萃取率如表2所示。
[0060] 实施例5
[0061] 萃取的具体的工艺条件见表1所示。采用图2所示的萃取系统进行煤液化残渣的萃 取，得到的重质液化油的重量与萃取率如表2所示。
[0062] 实施例6
[0063] 萃取的具体的工艺条件见表1所示。采用图2所示的萃取系统进行煤液化残渣的萃 取，得到的重质液化油的重量与萃取率如表2所示。
[0064] 实施例7
[0065] 萃取的工艺参数如表1所示，采用图2所示的萃取系统进行煤液化残渣的萃取，得 到的重质液化油的重量与萃取率如表2所示。
[0066] 实施例8
[0067] 萃取的工艺参数如表1所示，采用图2所示的萃取系统进行煤液化残渣的萃取，得 到的重质液化油的重量与萃取率如表2所示。
[0068] 实施例9
[0069] 萃取的工艺参数如表1所示，采用图2所示的萃取系统进行煤液化残渣的萃取，得 到的重质液化油的重量与萃取率如表2所示。
[0070] 实施例10
[0071] 萃取的工艺参数如表1所示，采用图2所示的萃取系统进行煤液化残渣的萃取，得 到的重质液化油的重量与萃取率如表2所示。
[0072] 实施例11
[0073] 萃取的工艺参数如表1所示，采用图2所示的萃取系统进行煤液化残渣的萃取，得 到的重质液化油的重量与萃取率如表2所示。
[0074] 实施例12
[0075] 萃取的工艺参数如表1所示，采用图2所示的萃取系统进行煤液化残渣的萃取，得 到的重质液化油的重量与萃取率如表2所示。
[0076] 对比例1
[0077] 将IOOkg煤直接液化残渣与500Kg第一萃取溶剂（馏程为< Il(TC)加入到搅拌釜 中，并使它们进行充分混合，充N2至I. OMPa，升温至100°C，以lOOr/min的搅拌速度搅拌30分 钟后得到混合物。然后进行加压热过滤，得到萃取液混合物Sl，送入常压蒸馏塔，切取<110 °C的馏份，回收第一萃取溶剂循环使用。塔底得到重质液化油35. lKg，然后与其它循环溶剂 和热处理副产油品混合后送入加氢装置。加氢操作条件为9.5MPa、365°C、反应液时空速 (LHSV) I. Oh—1，气液比850m3/t，加氢催化剂为Ni-W/ γ -Al2O3，加氢前后芳碳率差值为0.06， 满足煤直接液化工艺对循环溶剂的要求。将一级萃取得到的固体物质与250Kg第二萃取溶 剂(馏程为220〜260°C)加入到搅拌釜中，然后使它们进行充分混合。充N2气至1.5MPa，升温 至150°C，以lOOr/min的搅拌速度搅拌40分钟后得到混合物。然后进行加压热过滤，得到萃 取液混合物S2，送入常压蒸馏塔，切取220〜260°C的馏份，回收第二萃取溶剂供循环使用， 塔底得到沥青类物质25.4Kg。送入热处理单元，在440°C下进行干馏处理，得到重质油份 7.6Kg〇
[0078] 表 1
[0083] ^由表征上述的是实施例与对比例的萃取结果的表2可以得出：（1)与现有技术相 比，本申请的萃取方法采用简单的工艺流程，就可以获取与现有技术相同或者更高的萃取 率。（2)当夹带剂与超临界流体二氧化碳的质量比在10:100〜40:100,超临界萃取的温度在 40〜80 °C之间，超临界萃取的压力在30〜45MPa之间，分离的温度在30〜60°C之间，压力在3 〜6MPa之间，并且最后采用常压蒸馏或减压蒸馏时，萃取得到重质液化油的萃取效果较好。
[0084] 从以上的描述中，可以看出，本发明上述的实施例实现了如下技术效果：
[0085] 1)本申请的萃取系统，首先，利用超临界二氧化碳发生单元产生超临界二氧化碳 流体，其次，采用超临界二氧化碳流体对煤液化残渣进行萃取，超临界二氧化碳流体的扩散 能力是普通液体的100倍，因而具有很好的溶解能力，它能够迅速渗透进入微孔隙的物质， 进而实现对煤液化残渣快速、高效地萃取。该方法只利用超临界二氧化碳发生单元与萃取 单元就可以将重质液化油从煤液化残渣中萃取出来，工艺流程简单，克服了现有技术中萃 取煤液化残渣工艺流程复杂的问题。
[0086] 2)本申请的萃取方法利用上述萃取系统实施，与现有技术相比，该方法只利用超 临界二氧化碳流体就可以对煤液化残渣进行萃取，得到重质液化油，克服了现有萃取方法 的工艺流程较复杂的问题。
[0087] 以上所述仅为本发明的优选实施例而已，并不用于限制本发明，对于本领域的技 术人员来说，本发明可以有各种更改和变化。凡在本发明的精神和原则之内，所作的任何修 改、等同替换、改进等，均应包含在本发明的保护范围之内。
Claims (15)
1. 一种煤液化残渣的萃取系统，其特征在于，所述萃取系统包括： 超临界二氧化碳发生单元(10);以及 萃取单元(20)，与所述超临界二氧化碳发生单元（10)连通，其中，所述超临界二氧化碳发生单元(10)包括： 二氧化碳冷凝器(11)，将二氧化碳冷凝至超临界温度； 第一高压栗（12)，与所述二氧化碳冷凝器（I 1)连通，将来自所述二氧化碳冷凝器（I 1)的所述二氧化碳加压至超临界压力； 混合器（13)，与所述二氧化碳冷凝器（I 1)连通，将夹带剂和所述二氧化碳混合形成混合物； 加热器（14)，与所述混合器（13)和所述萃取单元（20)连通，加热来自所述混合器（13)的混合物。
2. 根据权利要求1所述的萃取系统，其特征在于，所述超临界二氧化碳发生单元（10)还包括第二高压栗（15)，所述第二高压栗（15)与所述混合器（13)连通将所述夹带剂栗入所述混合器(13)中。
3. 根据权利要求1所述的萃取系统，其特征在于，所述萃取系统还包括萃取物分离单元(30)，所述萃取物分离单元(30)与所述萃取单元(20)连通。
4. 根据权利要求3所述的萃取系统，其特征在于，所述萃取物分离单元(30)包括： 分离釜(31)，与所述萃取单元(20)连通，具有二氧化碳出口和液体出口；以及 蒸馏釜(32)，与所述分离釜(31)的液体出口连通，具有夹带剂出口。
5. 根据权利要求4所述的萃取系统，其特征在于，所述分离釜(31)通过所述二氧化碳出口与所述二氧化碳冷凝器（I 1)连通，优选所述蒸馏釜(32)通过所述夹带剂出口与所述混合器(13)连通。
6. —种煤液化残渣的萃取方法，其特征在于，所述萃取方法包括： 对煤液化残渣进行二氧化碳超临界萃取，得到含有所述煤液化残渣中的重质液化油的萃取液， 所述二氧化碳超临界萃取在夹带剂存在下进行。
7. 根据权利要求6所述的萃取方法，其特征在于，所述夹带剂为正已烷和/或煤液化轻 油。
8. 根据权利要求7所述的萃取方法，其特征在于，所述夹带剂与超临界状态的二氧化碳的重量比为10:100〜40:100。
9. 根据权利要求6所述的萃取方法，其特征在于，所述超临界萃取的温度在40〜80°C之间。
10. 根据权利要求9所述的萃取方法，其特征在于，所述超临界萃取的压力在30〜45MPa之间。
11. 根据权利要求6所述的萃取方法，其特征在于，所述煤液化残渣为粒径在0.2mm〜Imm之间的煤液化残渣粒子。
12. 根据权利要求7所述的萃取方法，其特征在于，所述萃取方法在完成所述超临界萃取后还包括： 步骤A，对所述萃取液进行分离，得到分离的混合液和所述二氧化碳；以及 步骤B，对所述混合液进行蒸馏，得到分离的所述夹带剂和所述重质液化油。
13. 根据权利要求12所述的萃取方法，其特征在于，所述分离的温度在30〜60°C之间，所述分离的压力在3〜6MPa之间。
14. 根据权利要求12所述的萃取方法，其特征在于，所述蒸馏为常压蒸馏或减压蒸馏。
15. 根据权利要求12所述的萃取方法，其特征在于，所述步骤A得到的所述二氧化碳和所述步骤B得到的所述夹带剂可以返回所述超临界萃取过程循环使用。
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