WO2016026421A1 - 溶剂分离油砂的装置 - Google Patents

溶剂分离油砂的装置 Download PDF

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WO2016026421A1
WO2016026421A1 PCT/CN2015/087325 CN2015087325W WO2016026421A1 WO 2016026421 A1 WO2016026421 A1 WO 2016026421A1 CN 2015087325 W CN2015087325 W CN 2015087325W WO 2016026421 A1 WO2016026421 A1 WO 2016026421A1
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organic solvent
solvent
separator
oil sands
extraction
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王平
曹鹏
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王平
曹鹏
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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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/04—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by extraction

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  • the invention relates to a device for separating bitumen from oil sands.
  • Natural oil sand is a petroleum conversion product. Petroleum oil is formed by penetrating into the ground. The light components are evaporated, and then oxidized by oxygen in the air under sunlight, and then polymerized to become asphalt minerals, mainly from asphaltenes. Resin and other colloidal materials, as well as a small amount of other mineral impurities such as metal and non-metal, natural oil sand is also called tar sand, heavy oil sand, tar sand.
  • the industrially used relatively mature is the hot alkaline washing method, which first pulverizes the oil sands and then sends them into the hot alkali. The mixture is stirred and mixed, and then the gas is introduced into the mixed slurry to float the bitumen. The bitumen is collected and diluted with an alkane to reduce the viscosity, and then sent to a refinery for refining to obtain various oil products.
  • This method is simple to operate, but it has the following problems: high energy consumption, large water consumption, serious environmental pollution, and opposition from governments and people around the world. It is extremely urgent to find environmentally friendly, economical and sustainable oil sands separation methods.
  • the solvent extraction technology is used to separate the asphalt in the oil sands, which has the following advantages: high separation efficiency, no water participation in the extraction process, saving water resources and avoiding subsequent water treatment problems; operating at normal temperature, low energy consumption The operation cost is low; the solvent is recycled, and the utilization efficiency is high; the extraction process and the transportation of the asphalt oil can be well coupled, the link of adding the intermediate is reduced, and the operation cost is further reduced.
  • the traditional solvent extraction technology also has some technical problems to be solved: efficient and economical solvents are not easy to obtain; solvents remaining in solid sand are difficult to recover.
  • Chinese patent CN101274303A reports a method for extracting oil sands using esters and the like as a solvent.
  • the liquid-solid separation of the extract is carried out by a drier and a centrifuge, the solid phase is directly backfilled, and the solvent is recycled, the process is simple, but Key problems such as solid processing are not well solved. If applied to large-scale industrial production, it will lead to secondary pollution problems;
  • CN101544902A a mixture of naphtha, isoamyl acetate and pentane mixed at 20:1:1
  • Solvent extraction of oil sands the extraction is divided into three levels, the extraction temperature of each level is controlled at 50 ° C, solvent recycling, the technology can obtain a higher extraction rate, but also the treatment of residual solids after extraction, and the entire process No solutions have been proposed for economic and environmental protection operations; in the 1960s and 1970s, US Patent No. 3,117,922 (1964), US 3,392,105 (1968);
  • a common problem encountered by the previous patents on the separation of oil sands using solvent extraction technology is the treatment of suspended microparticles in the residual sand and extract after extraction. Some techniques can achieve higher extraction. Efficiency, but can not solve the problem of solvent recovery in the residue, and some can solve the problem of solvent recovery in the residue, but the economic cost is too high to be industrialized, which is why solvent extraction technology has not been put into industrial use so far. Therefore, in order to obtain industrial application, the solvent extraction method must solve the problem of recovery of solvent and asphalt organic matter remaining in solids, and an important problem to solve the above problem is to provide a suitable device to ensure that the above problems can be minimized. The cost is realized. Therefore, designing a device for separating oil sands by solvent is an urgent problem to be solved.
  • the apparatus for separating oil sands by the solvent comprises:
  • a first agitation tank an upper portion of the first agitation tank is provided with an organic solvent I inlet;
  • a primary separator connected to the bottom of the agitation tank through a pipeline, an upper portion of the primary separator is provided with an extraction phase outlet, and the extraction phase outlet is connected to a subsequent refining process through a pipeline;
  • a second agitation tank connected to the bottom of the primary separator by a pipeline, and an upper portion of the second agitation tank is provided with an organic solvent II inlet;
  • a secondary separator connected to the bottom of the second agitation tank through a pipeline, the upper portion of the secondary separator is provided with an organic solvent I outlet;
  • a spiral dryer connected to the bottom of the secondary separator through a pipeline, the joint being located at the bottom of the spiral dryer;
  • a condenser connected to the material outlet of the screw dryer via a line, the condenser being provided with a condensate outlet.
  • the device of the invention can continuously operate the oil sands extraction process, save energy and reduce consumption, solves the problem of solvent recovery in the residual sand after extraction, has small environmental pollution, completely recycles the solvent, reduces intermediate links, and is applicable to oil sands ore.
  • Figure 1 is a schematic view showing the structure of the apparatus of the present invention.
  • the apparatus for separating oil sands by a solvent comprises:
  • the first agitation tank 3, the upper portion of the first agitation tank 3 is provided with an organic solvent I inlet 301;
  • the primary separator 4 is preferably a suspension separator; the structure of the term "suspension separator" is conventional and is described in detail in the relevant chemical engineering manual;
  • a second agitation tank 5 connected to the bottom of the primary separator 4 through a pipeline, the upper portion of the second agitation tank 5 is provided with an organic solvent II inlet 501;
  • a secondary separator 6 connected to the bottom of the second agitation tank 5 through a pipeline, an upper portion of the secondary separator 6 is provided with an organic solvent I outlet, preferably, the organic solvent I outlet is passed through a pipeline
  • the first agitation tank 3 is in communication, and the secondary separator 6 is preferably a suspension separator;
  • a spiral dryer 7 connected to the bottom of the secondary separator 6 through a pipeline, the junction is located at a lower portion of the spiral dryer 7;
  • a condenser 8 connected to the material outlet of the spiral dryer 7 through a pipeline, the condenser 8 is provided with a condensate outlet, preferably, the condensate outlet is passed through a pipeline and a second agitation tank (5) Connected
  • the method for extracting asphalt in oil sands by using the above device comprises the following steps:
  • the mixed slurry obtained in the step (1) is sent to the primary separator 4, and a solid-liquid separation is performed to separately collect the extracted phase and the raffinate phase, and the extracted phase is a mixture of the pitch and the organic solvent I,
  • the raffinate phase is a mixture of residual sand and organic solvent I;
  • the collected extract phase is sent to a subsequent refining process 24 to refine the extracted bitumen, and the recovered organic solvent I can be returned to the recycling;
  • the spiral dryer is a device commonly used in the field, and the specific structure can be referred to the chemical engineering manual.
  • the gas mixture containing the organic solvent II flows out from the upper portion of the spiral dryer 7, condenses in the condenser 8, and collects the condensed organic solvent II, which can be recycled;
  • the separated solid residue containing clay and fine sand separated from the bottom of the spiral dryer 7 is sent to the brick factory for the production of environmentally-resistant and anti-vibration structural bricks.
  • the organic solvent I is a mixture of one or more of an alkane and an alcohol or an aldehyde;
  • the alkane preferably contains an alkane having 8 to 12 carbon atoms
  • the alcohol is preferably n-butanol, isobutanol or neopentyl alcohol;
  • the aldehyde is preferably isobutyraldehyde.
  • oil sands refer to sediment sands rich in natural asphalt and are therefore also referred to as "asphalt sands".
  • Oil sands are essentially a mixture of bitumen, sand, rich ore and water, of which:
  • the mixed slurry obtained in the step (1) is subjected to primary solid-liquid separation, and the extracted phase and the raffinate phase are separately collected, and the extracted phase is extracted.
  • the raffinate phase is a mixture of primary residual sand and organic solvent I;
  • the extracted phase is collected, sent to a subsequent refining process, and the bitumen is extracted through a refining process, and the recovered organic solvent I can be returned to the recycling;
  • the organic solvent II is selected from the group consisting of a mixture of an alkane and naphtha, gasoline or reformed gasoline;
  • the alkane preferably contains an alkane having 8 to 12 carbon atoms
  • the product ratio of the raffinate phase to the organic solvent II body is 2 to 3:1.
  • the solvent is used to separate the oil sands.
  • the weight of the asphalt is 20%.
  • the mass ratio of organic solvent I to oil sands is 2:1;
  • the separated extraction phase is sent to a subsequent refining step 24, and the asphalt and the organic solvent I are separated, and the organic solvent I is recycled;
  • the separated residual coarse solids are sent to a spiral dryer 7 for solvent removal treatment;
  • the screw dryer 7 After the screw dryer 7 is heated to 100 ° C, the gas mixture containing the solvent vapor is sent to the condenser 8 for condensation, and the organic solvent II is separated.
  • the solid residual sand containing clay and fine sand obtained by the spiral dryer 7 is sent to the brick factory for the production of environmentally-resistant and anti-vibration structural bricks.
  • the obtained oil sand bitumen has an extraction rate of 100% and a solvent recovery rate of 100%; the crude residual sand has a solvent content of 0, the bitumen content is 0, and all the residual sand is utilized.
  • the solvent is used to separate the oil sands.
  • the weight of the asphalt is 30%.
  • the mass ratio of organic solvent I to oil sands is 3:1;
  • the separated extraction phase is sent to a subsequent refining step 24, and the asphalt and the organic solvent I are separated, and the organic solvent I is recycled;
  • the separated residual coarse solids are sent to a spiral dryer 7 for solvent removal treatment;
  • the screw dryer 7 After the screw dryer 7 is heated to 100 ° C, the gas mixture containing the solvent vapor is sent to the condenser 8 for condensation, and the organic solvent II is separated.
  • the solid residual sand containing clay and fine sand obtained by the spiral dryer 7 is sent to the brick factory for production of environmentally-resistant and anti-vibration structural bricks;
  • the obtained oil sand bitumen has an extraction rate of 100% and a solvent recovery rate of 100%; the crude residual sand has a solvent content of 0, the bitumen content is 0, and the residual sand is fully utilized.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Extraction Or Liquid Replacement (AREA)
  • Working-Up Tar And Pitch (AREA)

Abstract

本发明公开了一种溶剂分离油砂的装置，包括：第一搅拌槽，与所述的搅拌槽相连接的一次分离机，与一次分离机的底部相连接的第二搅拌槽，第二搅拌槽上部设有有机溶剂Ⅱ入口，与第二搅拌槽底部相连接的二次分离机，二次分离机上部设有有机溶剂Ⅰ出口；与二次分离机相连接的螺旋式干燥器，与螺旋式干燥器的物料出口相连接的冷凝器。本发明的装置，能够对油砂提取过程连续操作，节能降耗，解决了提取后残砂中的溶剂回收问题，环境污染小，溶剂完全循环使用，减少了中间环节，可用于油砂矿开采现场的完整油砂分离的装置。

Description

溶剂分离油砂的装置 技术领域
本发明涉及分离油砂中沥青的装置。
背景技术
天然油砂是石油的转化物，石油原油渗透到地面而形成，其中轻质组分被蒸发，进而在日光照射下被空气中的氧气氧化，再经聚合而成为沥青矿物，主要由沥青质、树脂等胶质，以及少量的金属和非金属等其它矿产物杂质组成，天然油砂又称焦油砂、重油砂、沥青砂。
目前，天然油砂占据了世界石油储量的66％，主要分布在加拿大，目前加拿大估计可采量还有3150亿桶原油，仅次于沙特阿拉伯，其它地区分布在美国、俄罗斯、委内瑞拉、印度尼西亚、法国、瑞士、意大利、特立尼达和多巴哥、阿尔巴尼亚、蒙古，中国的天然油砂矿主要分布在四川、内蒙古、新疆、辽宁等地区。
目前，就开采而言，主要有热碱水洗工艺、溶剂提取工艺、热裂解工艺等几种，目前工业上使用比较成熟的是热碱水洗法，该技术先将油砂粉碎，再送入热碱液中混合搅拌，然后向混合浆液中通入气体使沥青浮选上来，收集沥青并加入烷烃稀释以降低其粘度后，送往炼厂进行精炼获得各种油产品。这种方式操作简单，但存在以下问题：能耗高、耗水量大、对环境污染严重，受到世界各国政府和人民的反对。寻找环保、经济、可持续发展的油砂分离方法迫在眉睫。
采用溶剂提取技术，分离油砂中沥青的方法，具备如下优点：分离效率高，提取过程不需要水的参与，既节约水资源，也避免了后续的水处理问题；常温下操作，能耗低，操作成本低；溶剂循环使用，利用效率高；另外提取过程和沥青油的输送可以很好耦合，减少了中间添加稀释剂的环节，进一步降低操作成本。但是，传统的溶剂提取技术也存在一些有待解决的技术问题：高效、经济的溶剂不易于获得；残留于固体沙粒中的溶剂回收难度较大等。
中国专利CN101274303A报道了一种使用酯类等作为溶剂对油砂进行提取的方法，采用滤干机和离心机对提取液进行液固分离，固相直接回填，溶剂循环使用，过程简单，但关于固体处理等关键问题没有很好的解决，若应用于大批量的工业生产中，将会导致环境二次污染问题；
CN101544902A公开的技术，采用石脑油、乙酸异戊酯、戊烷按照20:1:1进行混合的混合 溶剂对油砂进行提取，提取分为三级，各级提取温度均控制在50℃，溶剂循环利用，该技术可获得较高提取率，但同样关于提取后残留固体的处理，以及整个工艺的经济、环保运行等问题没有提出解决办法；在20世纪六七十年代，美国专利US3117922(1964)，US3392105(1968)；
US4046669(1969)，US4046668(1977)等提出使用有机溶剂如甲苯、石脑油等对油砂进行提取，采用离心等方法对提取液进行液固分离；
US4036732(1977)指出采用C5～C9的脂肪烃对油砂进行提取，使用一定量的水对提取后的沙粒进行洗涤，而悬浮于提取液中的细颗粒采用离心的方法进行分离；US3553099也指出采用有机溶剂先提取油砂，然后用水洗的方法处理残砂；US4139450(1979)指出采用热甲苯对油砂进行处理，同时采用两级离心的方法对提取液进行液固分离；US4347118(1982)中指出采用戊烷为溶剂对油砂进行提取，然后采用两级流化床对残留沙粒进行干燥，没有对细颗粒的处理；Williams等(US4108760，1978)采用超临界温度在200℃以内的有机物作为溶剂，于370℃至450℃对油砂进行提取，获得较好的效果；Angelov，G.等(US4498971，1984)则提出采用液氮对油砂进行冷冻破碎来对其进行分离，提取其中的沥青；
US4929341(1990)报道了硫酸铵、丙酮、硫酸等可以促进有机溶剂(四氯乙烯、四氯化碳、石油醚、甲苯、苯等)对油砂的提取效果，但此技术需进行4小时左右方可取得较好效果。
综合前人关于使用溶剂提取技术对油砂进行分离的专利技术，所遇到的一个共性问题就是关于提取后残砂和提取液中悬浮微颗粒的处理问题，有的技术能达到较高的提取效率，但无法解决残留物中溶剂回收的问题，有的可以解决残留物中溶剂回收问题，但经济代价太高，无法工业化实施，这些也是为什么溶剂提取技术至今为止一直无法真正投入工业使用的原因；因此，溶剂提取法要获得工业化运用，必须解决残留于固体中溶剂和沥青有机物的回收问题，而解决上述问题的一个重要的课题，是提供一种合适的装置，以确保上述的问题能够以最小的代价实现，因此，设计一种溶剂分离油砂的装置，是人们所十分迫切需要解决的课题。
发明内容
本发明的目的是提供一种溶剂分离油砂的装置，以克服现有技术存在的上述缺陷，满足相关领域发展的需要。
所述的溶剂分离油砂的装置，包括：
第一搅拌槽，所述第一搅拌槽的上部设有有机溶剂Ⅰ入口；
与所述的搅拌槽的底部通过管线相连接的一次分离机，所述一次分离机上部设有提取相出口，所述提取相出口通过管线与后续的精炼工序相连通；
术语“悬液分离器”的结构为常规的，在相关的化学工程手册上有详细的描述；
与所述的一次分离机的底部通过管线相连接的第二搅拌槽，所述第二搅拌槽的上部设有有机溶剂Ⅱ入口；
与所述的第二搅拌槽的底部通过管线相连接的二次分离机，所述二次分离机的上部设有有机溶剂Ⅰ出口；
与所述二次分离机的底部通过管线相连接的螺旋式干燥器，连接处位于螺旋式干燥器的底部；
与所述的螺旋式干燥器的物料出口通过管线相连接的冷凝器，所述冷凝器设有冷凝液出口。
本发明的装置，能够对油砂提取过程连续操作，节能降耗，解决了提取后残砂中的溶剂回收问题，环境污染小，溶剂完全循环使用，减少了中间环节，是可用于油砂矿开采现场的完整油砂分离的装置。
附图说明
图1为本发明的装置的结构示意图。
具体实施方式
参见图1，所述的溶剂分离油砂的装置，包括：
第一搅拌槽3，所述第一搅拌槽3的上部设有有机溶剂Ⅰ入口301；
与所述的搅拌槽3的底部通过管线相连接的一次分离机4，所述一次分离机4上部设有提取相出口402，所述提取相出口402通过管线与后续的精炼工序24相连通，所述一次分离机4优选为悬液分离器；术语“悬液分离器”的结构为常规的，在相关的化学工程手册上有详细的描述；
与所述的一次分离机4的底部通过管线相连接的第二搅拌槽5，所述第二搅拌槽5的上部设有有机溶剂Ⅱ入口501；
与所述的第二搅拌槽5的底部通过管线相连接的二次分离机6，所述二次分离机6的上部设有有机溶剂Ⅰ出口，优选的，所述有机溶剂Ⅰ出口通过管线与第一搅拌槽3相连通，二次分离机6优选为悬液分离器；
与所述二次分离机6的底部通过管线相连接的螺旋式干燥器7，连接处位于螺旋式干燥器7的下部；
与所述的螺旋式干燥器7的物料出口通过管线相连接的冷凝器8，所述冷凝器8设有冷凝液出口，优选的，所述冷凝液出口通过管线与第二搅拌槽(5)相连接；
采用上述装置，提取油砂中沥青的方法，包括如下步骤：
(1)将油砂与有机溶剂Ⅰ送入第一搅拌槽3混合提取，获得有机溶剂Ⅰ与油砂的混合浆液；
(2)将步骤(1)获得的混合浆液，送入一次分离机4，进行一次固液分离，分别收集提取相和提余相，所述提取相为沥青与有机溶剂Ⅰ的混合物，所述提余相为一次残砂与有机溶剂Ⅰ的混合物；
收集的提取相，送入后续的精炼工序24精炼提取出沥青，回收的有机溶剂Ⅰ可以返回循环使用；
(3)将步骤(2)收集的提余相与有机溶剂Ⅱ送入第二搅拌槽5，进行二次提取；
(4)二次固液分离获得的残留粗颗粒固体与机溶剂Ⅱ的混合物，送入螺旋式干燥器7的下部，对残留粗颗粒固体进行干燥脱溶剂；
所述螺旋式干燥器为本领域通用的设备，具体结构可参见化学工程手册。
含有机溶剂Ⅱ的气体混合物，由螺旋式干燥器7的上部流出，在冷凝器8中冷凝，收集冷凝后的有机溶剂Ⅱ，可循环使用；
螺旋式干燥器7底部分离出来的分离出来的含粘土、细沙粒的固体残砂送至砖厂，用于生产环保抗震结构砖。
所述的有机溶剂Ⅰ为烷烃与醇类或醛类中的一种以上的混合物；
醇类或醛类与烷烃的体积比为：醇类或醛类∶烷烃＝1～8∶1；
所述烷烃优选含有8～12个碳原子的烷烃；
所述醇类优选正丁醇、异丁醇或新戊醇；
所述醛类优选异丁醛。
所述油砂是指富含天然沥青的沉积砂，因此也称为“沥青砂”。油砂实质上是一种沥青、沙、富矿粘土和水的混合物，其中：
Figure PCTCN2015087325-appb-000001
将步骤(1)获得的混合浆液，进行一次固液分离，分别收集提取相和提余相，所述提取相 为沥青与有机溶剂Ⅰ的混合物，所述提余相为一次残砂与有机溶剂Ⅰ的混合物；
收集提取相，送入后续的精炼工序，经由精炼工序提取出沥青，回收的有机溶剂Ⅰ可以返回循环使用；
(3)将步骤(2)收集的提余相与有机溶剂Ⅱ混合，进行二次提取，40～120℃提取10～15min，获得有机溶剂Ⅰ、有机溶剂Ⅱ和含残砂的混合浆液，然后进行二次固液分离，收集二次固液分离的清液，为有机溶剂Ⅰ，可循环使用；
所述的有机溶剂Ⅱ选自烷烃与石脑油、汽油或重整汽油的混合物；
烷烃与石脑油、汽油或重整汽油的体积比为：烷烃∶石脑油、汽油或重整汽油＝4～8∶1；
所述烷烃优选含有8～12个碳原子的烷烃；
提余相与机溶剂Ⅱ体的积比为2～3∶1。
实施例1
采用图1的流程，采用溶剂分离油砂，油砂中，沥青的重量含量为20％
将经由螺旋滚筒高温水破碎除砂器破碎至大小为20mm的油砂颗粒5kg，送入一次搅拌槽3与有机溶剂Ⅰ于25℃下混合，搅拌10min，然后送入一次悬液分离器4，进行液固分离；
所述有机溶剂Ⅰ为正辛烷与异丁醛的混合物，体积比为正辛烷：异丁醛＝1:5；
有机溶剂Ⅰ与油砂的质量比为2:1；
分离出的提取相送往后续的精炼工序24，分离出沥青和有机溶剂Ⅰ，有机溶剂Ⅰ循环使用；
分离出的提余相，送入二次搅拌槽5中，同时加入有机溶剂Ⅱ，提余相与机溶剂Ⅱ体的积比为：提余相：有机溶剂Ⅱ＝2∶1；
于25℃下洗涤提取10min，获得有机溶剂Ⅰ、有机溶剂Ⅱ和含残砂的混合浆液，然后送入二次旋液分离器6，进行液固分离，分离出的液相为有机溶剂Ⅰ，可循环使用；
所述的有机溶剂Ⅱ为正辛烷与石脑油的混合物，正辛烷∶石脑油＝5∶1；
分离出的残留粗颗粒固体，送入螺旋式干燥器7，进行脱溶剂处理；
螺旋式干燥器7加热至100℃后，含有溶剂蒸汽的气体混合物送入冷凝器8进行冷凝，分离出有机溶剂Ⅱ。螺旋式干燥器7获得的含粘土、细沙粒的固体残砂送至砖厂，用于生产环保抗震结构砖。
所得油砂沥青的提取率100％，溶剂回收率100％；粗残砂中含溶剂量为0、含沥青量为0，残砂全部得到利用。
实施例2
采用图1的装置，采用溶剂分离油砂，油砂中，沥青的重量含量为30％
将经由螺旋滚筒高温水破碎除砂器破碎至大小为20mm的油砂颗粒5kg，送入一次搅拌槽3与有机溶剂Ⅰ于20℃下混合，搅拌提取15min，然后送入一次悬液分离器4，进行液固分离；
所述有机溶剂Ⅰ为正辛烷与异丁醛的混合物，体积比为正辛烷：异丁醛＝1:8；
有机溶剂Ⅰ与油砂的质量比为3:1；
分离出的提取相送往后续的精炼工序24，分离出沥青和有机溶剂Ⅰ，有机溶剂Ⅰ循环使用；
分离出的提余相，送入二次搅拌槽5中，同时加入有机溶剂Ⅱ，提余相与机溶剂Ⅱ体的积比为：提余相∶机溶剂Ⅱ＝3:1；
所述的有机溶剂Ⅱ为正辛烷与汽油的混合物，正辛烷∶汽油＝8∶1；
于20℃下洗涤提取15min，获得有机溶剂Ⅰ、有机溶剂Ⅱ和处理残砂的混合浆液，然后送入二次旋液分离器6，进行液固分离，分离出的液相为有机溶剂Ⅰ，可循环使用；
分离出的残留粗颗粒固体，送入螺旋式干燥器7，进行脱溶剂处理；
螺旋式干燥器7加热至100℃后，含有溶剂蒸汽的气体混合物送入冷凝器8进行冷凝，分离出有机溶剂Ⅱ。螺旋式干燥器7获得的含粘土、细沙粒的固体残砂送至砖厂，用于生产环保抗震结构砖；
所得油砂沥青的提取率100％，溶剂回收率100％；粗残砂中含溶剂量为0、含沥青量为0，残砂得到全部利用。

Claims (6)

  1. 溶剂分离油砂的装置，其特征在于，包括：
    第一搅拌槽(3)，所述第一搅拌槽(3)的上部设有有机溶剂Ⅰ入口(301)；
    与所述的搅拌槽(3)的底部通过管线相连接的一次分离机(4)，所述一次分离机(4)上部设有提取相出口(402)；
    与所述的一次分离机(4)的底部通过管线相连接的第二搅拌槽(5)，所述第二搅拌槽(5)的上部设有有机溶剂Ⅱ入口(501)；
    与所述的第二搅拌槽(5)的底部通过管线相连接的二次分离机(6)，所述二次分离机(6)的上部设有有机溶剂Ⅰ出口；
    与所述二次分离机(6)的底部通过管线相连接的螺旋式干燥器(7)，连接处位于螺旋式干燥器(7)的下部；
    与所述的螺旋式干燥器(7)上部的物料出口通过管线相连接的冷凝器(8)，所述冷凝器(8)设有冷凝液出口。
  2. 根据权利要求1所述的溶剂分离油砂的装置，其特征在于，所述提取相出口(402)通过管线与后续的精炼工序(24)相连通。
  3. 根据权利要求1所述的溶剂分离油砂的装置，其特征在于，所述一次分离机(4)为悬液分离器。
  4. 根据权利要求1所述的溶剂分离油砂的装置，其特征在于，所述二次分离机(6)上部的有机溶剂Ⅰ出口通过管线与第一搅拌槽(3)相连通。
  5. 根据权利要求1所述的溶剂分离油砂的装置，其特征在于，二次分离机(6)为悬液分离器。
  6. 根据权利要求1所述的溶剂分离油砂的装置，其特征在于，所述冷凝液出口通过管线与第二搅拌槽(5)相连接。
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