CN105143409A - 处理烃基重质残留物的方法 - Google Patents
处理烃基重质残留物的方法 Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 59
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 20
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 20
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 19
- 230000008569 process Effects 0.000 title claims abstract description 12
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 claims abstract description 42
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 claims abstract description 21
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims abstract description 18
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- 125000000217 alkyl group Chemical group 0.000 claims description 3
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- 229910052723 transition metal Inorganic materials 0.000 claims description 2
- 150000003624 transition metals Chemical class 0.000 claims description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims 2
- 239000000126 substance Substances 0.000 claims 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims 1
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- 239000010941 cobalt Substances 0.000 claims 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims 1
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Abstract
处理烃基重质残留物(1),特别是处理具有高沥青质含量的沥青残留物,的方法,其包括下面的操作:A)将待处理的重质残留物置于325-500℃的温度;B)在压力等于或者低于大约0.1bara和温度等于或者低于450℃的环境中,使待处理的重质残留物经历基本上绝热膨胀,来从该待处理的重质残留物中分离第一较低挥发性馏分(17),该第一较低挥发性馏分在大气压时下沸点等于或者高于540℃,并且它的固体和/或无水残留物主要包含不溶于戊烷的沥青质和/或不溶于四氢呋喃的其他残留物。它允许更有效的冲洗,以及在极其简单的设备中启动所述方法,而无需离心分离。
Description
发明领域
本发明涉及一种处理烃基残留物的方法。
本发明的方法和设备特别适于处理和促进烃基残留物,特别是具有高沥青质含量的沥青残留物的使用、管理和处置,所述残留物是在具有高分子量或者在任何情况中具有高C/H比的有机残留物的之前的转化过程中作为副产物而获得的,例如油或者更通常的重质烃,可能已经部分脱沥青的蒸馏残留物,来自于沥青砂的沥青,来源于煤和油页岩的油。
现有技术
高分子量有机残留物例如重质油(例如可能已经部分脱沥青的蒸馏残留物),来自于沥青砂的油,来源于煤和油页岩的油,的转化方法是目前已知的。该转化是通过降低待处理的残留物的分子量,和增加它们的H/C比来进行的。转化方法的例子(其组合了反应性链段在催化剂存在下的裂化和氢化反应)描述在文献US5932090,EP2158304,EP2155835,EP2291238中。
一种极其致密的沥青残留物是作为该转化的副产物而获得的,其在标准条件下具有粘糊的浓度,且因此极难管理用于运输、销售、处置或者可能再用于相同的生产位置。这种沥青残留物包含有机馏分,其通常具有甚至更高的分子量,和甚至更稠的焦炭和无机化合物馏分,相对于进入催化氢化裂解方法的残留物而言。
焦炭和无机残留物的含量形成了THFis,即,不溶于四氢呋喃的材料馏分。
沥青残留物是以相当大的量生产的:在能够精炼200,000桶/天原油的石化厂,例如依靠催化氢化裂解的有机残留物的相关转化工厂能够生产60,000桶/天。
所以便利的是将沥青残留物转化成更高品质的可以重新使用的产品,例如作为可燃烧的或者商业燃料,或者转化成惰性产品,其更易于管理、处置和对环境较少有害。
专利US3928170描述了一种方法(称作EUREKA方法),用于在1.1-3barg的压力和350-450℃的反应区域温度下,依靠热裂解在底部油残留物的蒸气流中生产沥青;该反应器之前是用于预热加料的炉子,和之后是产物分离区。沥青是从裂解反应器底部提取的,该反应器半分批运行来避免在预热阶段形成焦炭。但是这种方法不能令人满意的处理具有特别高的浓度沥青质的底部残留物或者不溶于四氢呋喃的残留物。
专利US4477334描述了一种方法,在其中重质烃可以在连续裂解方法中转化,不形成焦炭,而形成作为副产物的沥青。该溶剂脱沥青方法在接近于从沥青质组分中分离软沥青组分的那些关键条件的条件下,使用了溶剂(通常丙烷或丁烷):将沥青质馏分(其也可包含某些百分比的固体)再循环到所述方法,而软沥青馏分(富含DAO,脱沥青油)在通过在超临界条件下萃取分离溶剂后,形成了产物。在所讨论的生产浓缩沥青的情况中,这种方法代表了与溶剂脱沥青相反,因为它是待萃取的沥青质组分(富含固体相),并且软沥青组分是再循环的。
应用这种方法的困难是由在超临界条件下使用更多的塔来管理溶剂的循环组成的。
离心分离的局限之一是最大运行温度不能超过150℃。在这些条件下,可能存在着与浓缩流的移动和排放有关的问题,而轻质相(其再循环到反应区)仍然富含沥青质组分,其危害了转化设备的性能。
本发明的一个目标因此是克服现有技术的上述缺点,特别是通过提供一种方法,将高分子量有机残留物以前的转化方法的沥青和糊状残留物转化成更易于和方便再用和处置的产物。
发明内容
根据本发明,这个目标是用具有权利要求1的特征的方法来实现的。
本发明另外的特性是从属权利要求的目标。
对本领域技术人员来说,采用本发明可获得的优点通过参考附图所示的具体的非限定性实施方案的以下的详细说明将变得显而易见。
附图列示
图1显示了根据本发明具体的实施方案处理沥青质残留物的方法的方案;
图2显示了图1的设备的排出器的方案。
具体实施方式
在本说明书中,除非另有规定,否则表述“化合物X主要含有物质Y”应当解释为表示化合物X包含至少50重量%的物质Y。
图1,2涉及用于处理沥青状或者含沥青的残留物的设备,该残留物是在具有高分子量或者在任何情况中具有高C/H比的有机残留物的转化方法中作为副产物来获得的,例如重质油例如可能已经部分脱沥青的蒸馏残留物,来自于沥青砂的沥青,来源于煤和油页岩的油。
所述设备是用整体附图标记100来表示的。附图标记1表示供料流,其优选是底部排污,例如来自于例如在文献US5932090,EP2158304,EP2155835,EP2291238中所述的重质油转化设备的真空蒸馏塔,或者来自于依靠沸腾床催化氢化裂解或者其他裂解方法的重质油的其他转化方法。该供料流1的底部排污是固-液悬浮液,粘性的,但是在合适的温度虾可以泵送。
所述的供料流(1)中C5沥青质(不溶于正戊烷的沥青质)的含量是20-45%,而THFis是10-20%。
依靠氢化裂解的可能的转化方法的催化剂可以例如是基于一种或多种过渡金属例如Ni、Co、Mo,优选钼。
供料流1的温度可以例如是320-350℃和更优选320-330℃,目的是促进该流体的泵送性。在进入炉子3之前,将流1优选通过引入过热的水蒸气2,例如在大约350℃下的蒸气流量而加热和流化。水蒸气的引入还防止了在炉子中形成焦炭。
该水蒸气流量引入前优选是底部排污1的流量的0.5-2重量%,和优选是底部排污流量的大约1重量%。
供料流1’优选随后通过将它例如引入到炉子3中来进一步加热到大约325-500℃。即将引入分离器6的流4的温度可以基本上与炉子3内部温度相同,和优选等于或者低于480℃。流4可例如是三相固体-液体-蒸气流。
在炉子3中,优选压力高于大气压,更优选是1-2bara和甚至更优选是1.3-2bara。
这个压力优选与即将经历下文所述的绝热膨胀的流4的压力相同。
在本说明书中,除非另有规定,否则压力值应当被认为是绝对压力值,并且与大气压无关。
根据本发明的一方面,离开炉子3的流4在压力等于或者低于大约0.1bara和温度等于或者低于450℃的环境中经历了基本上绝热膨胀,来从待处理的重质残留物中分离第一较低挥发性馏分17,它在大气压下的沸点等于或者高于540℃和它的固体和/或无水残留物主要包含不溶于戊烷的沥青质和/或不溶于四氢呋喃的其他残留物。
还优选从重质残留物中分离第二较高挥发性馏分7,其主要由软沥青和在大气压下沸点等于或者低于540℃的其他烃组成。
该基本上绝热膨胀优选依靠穿过复合阀(laminationvalve)的基本上瞬时的膨胀(闪蒸)来进行。该绝热膨胀优选在包含密封容器的第一分离器6中进行,其中超压(abovepressure)等于或者低于0.1bara。更优选在分离器6中存在着等于或者低于0.04bara的压力。
上述最大温度450℃是在分离器6整体体积上的平均值。流4优选在温度等于或者低于400℃,和更优选等于或者低于390℃的环境中进行基本上绝热膨胀。
该闪蒸或者在任何情况中绝热膨胀有利地在密封容器上部或者在任何情况中在第一分离器6中进行,而将汽提流5,优选水蒸气流,引入它的下部中。
取决于运行条件(汽提蒸气流量5和/或闪蒸室6的温度),重质流中沥青质-THFi馏分可以在75-94%变化。
汽提蒸气5和底部排污流量1之间的比例是0.03-0.75,更优选0.03-0.5。
该第二较高挥发性馏分7与大部分汽提流5一起优选从第一分离器6排出,到达排出器8。排出器8有利的是图2的类型,即,装备有文丘里管,其吸入流7,引入到文丘里管的窄区,并且将它从管道8逐出,这取决于合适的动力流体9(例如蒸气)的流量,其从管道9’进入文丘里管。所以通过作用于进入文丘里管的动力流体9的流量,可以控制第一分离器6中的真空度。
更优选的,可以使用多步骤排出器系统,这取决于在闪蒸室中所获得的真空度。
流10(含有第二较高挥发性馏分7,汽提流5和动力流体9)随后例如依靠热交换器11来冷却,以冷凝较重的相,然后到达第二分离器13。
为了获得更有效的冷凝,交换器11在这样的温度运行,即,离开它的流12优选处于50℃。
第二分离器13从流12中分离了下面的产物:
-基于重质烃14的第一流,其富含脱沥青的重质油(DAO),软沥青和沸点等于或者高于540℃的其他烃;
-第二气态流15,其基于轻质烃和沸点低于540℃;和
-第三流16,其主要由冷凝水组成。
第一流14可以有利的再引入设备100上游的重质油精炼或者转化循环中,例如真空蒸馏塔中。第二气态流15可以例如作为燃料,推进剂或者其他市售品来销售。
在离开排出器的冷凝系统后,气态流15可以送到底部排污。
第一较低挥发性馏分17(其富含沥青质和贫含软沥青和其他轻质烃,几乎含有给料的全部沥青质,和具有取决于运行条件的6-25%范围内变化的软沥青和其他轻质烃的组成)在收集于第一分离器6的底部上之后,可以通过重力,依靠运行机或者再加压袋倾到到冷却的传送带18上,并且在其上冷却和转化成颗粒固体。在表面上骤冷冷却的带18之后,第一较低挥发性馏分17非常快速的凝固和碎裂。为此目的,冷却的传送带18的表面优选保持在等于或者低于大约100℃,和更优选等于或者低于大约50℃的温度。
同样出于这个目的,第一较低挥发性馏分17优选是在相对高的温度,例如等于或者高于315℃和甚至更优选315-480℃,沉积到传送带18上,或者在任何情况中从分离器6中排出。
这些高温度促进了其的排出作业。附图标记19表示颗粒形式的凝固的沥青残留物。因为它处于颗粒形式,而非糊或者淤浆形式,因此该沥青残留物19可以直接包装(例如在金属桶中)和商业化,或者在任何情况中明显更容易的管理。颗粒沥青残留物可以直接用作例如用于道路表面的惰性产品或者用于鼓风炉的燃料或者其他工业炉子。
绝热膨胀(优选闪蒸或者在任何情况中足够快的)和高真空度环境(膨胀在其中发生)的组合允许处理以前回收处理的残留物(具有特别高的沥青质和无机化合物含量),使得它们极其有效的分离成a)第一馏分,极其富含软沥青,液态或者气态烃和极其贫含沥青质,和b)第二馏分的在室温下的固体,其相当大地富含沥青质和无机残留物和极其贫含软沥青和液态或气态烃(在标准温度和压力)。
更具体的,本发明的方法特别适于处理来自于油或者烃处理方法的残留底部排污流,其中所述残留物包含至少30重量%,和甚至超过50重量%的不溶于戊烷的沥青质和/或不溶于四氢呋喃的其他残留物(不必需是有机的)。
待处理的重质残留物可以优选具有20-45重量%的C5-沥青质含量和10-20重量%的THFi含量。
较低挥发性馏分17的不溶于四氢呋喃的固体和沥青质的含量可以容易地达到和恒定保持在非常高的浓度,例如75-94重量%,或者在任何情况中超过75重量%。另一方面,本发明使得第二较高挥发性馏分7变得更贫含沥青质。
分离器6可以包含真空塔或者由真空塔组成,重质馏分可以从其底部萃取,轻质馏分从侧面萃取。含有水蒸气和不可冷凝的产物的流是从该塔的顶部萃取的,其被送到排出器8。来源于排出器8的分离的基于重质烃14的流可以与真空塔的侧面馏分合并(参见第18段)。
下面的结果提供了用本发明可获得的分离的效果的更好的证明,其获自涉及设备100的数字模拟,假定分离器6是适于在单个分离步骤中进行真空闪蒸的容器。
数字实施例1-8
在实施例1-4中,设备100处于以下条件下:
a.1)分离器6中的压力P6:0.02bara;
b.1)供料流1的组成:
-烃和通常沸点低于500℃的馏分(表中的500-):8重量%;
-烃和通常沸点为500-540℃的馏分(表中的500-540):14.2重量%;
-烃和通常沸点高于540℃的馏分,基本上可确定为软沥青馏分(表中的540+):28.4重量%;
-不溶于戊烷,但是可溶于四氢呋喃的沥青质馏分(表中的ASF-C5):29.4重量%;
-固体残留物,含有焦炭,其他有机和/或可能无机馏分例如金属硫化物和不溶于四氢呋喃的其他催化残留物(表中的THFis):20重量%;
d.1)过热蒸气2和汽提蒸气5的温度:350℃;
e.1)过热蒸气2的压力:4bara;
f.1)过热蒸气2和汽提蒸气5的流量:50kg/h。
下面的值是以前面的参数在设备100上获得的:
表1
例子1 | 例子2 | 例子3 | 例子4 | |
Q1,kg/h | 4643 | 4637 | 4641 | 4637 |
Q2+Q5,kg/h | 1000 | 1000 | 3000 | 3000 |
T3,℃ | 423 | 365 | 394 | 326 |
炉子3的热需求,MMKcal/h | 0.29 | 0.12 | 0.20 | 0.01 |
T6,℃ | 386 | 340 | 394 | 326 |
Q17总计,kg/h | 2429 | 2927 | 2428 | 2927 |
从Q1分离的% | 52.3 | 63.1 | 52.3 | 63.1 |
底部产物17的组成[wt%] |
500- | 0.6 | 0.19 | 0.04 | 0.13 |
500-540 | 0.37 | 1.37 | 0.29 | 1.12 |
540+ | 5.75 | 20.30 | 5.66 | 20.60 |
ASF-C5 | 55.58 | 46.46 | 55.76 | 46.47 |
THFis | 38.24 | 31.68 | 38.22 | 31.68 |
Q7,kg/h | 3214 | 2709 | 5212 | 4709 |
流7的组成[wt%] | ||||
H2O | 31.1 | 36.91 | 57.55 | 63.70 |
500- | 11.51 | 13.49 | 7.10 | 7.80 |
500-540 | 20.23 | 22.88 | 12.51 | 13.32 |
540+ | 36.78 | 26.71 | 22.72 | 15.17 |
ASF-C5 | 0.37 | 0.02 | 0.12 | 0.01 |
THFis | 0 | 0 | 0 | 0 |
在实施例5-8中,设备100处于下面的条件下:
a.2)分离器6中的压力P6:0.01bara;
b.2)供料流1的组成:同实施例1-4
下面的值是以前面的参数在设备100上获得的:
表2
例子5 | 例子6 | 例子7 | 例子8 | |
Q1,kg/h | 4650 | 4637 | 4645 | 4637 |
Q2+Q5,kg/h | 1000 | 1000 | 3000 | 3000 |
T3,℃ | 479 | 415 | 459 | 383 |
炉子3的热需求,MMKcal/h | 0.45 | 0.26 | 0.39 | 0.17 |
T6,℃ | 437 | 385 | 402 | 354 |
Q17总计,kg/h | 2430 | 2927 | 2429 | 2927 |
从Q1分离的% | 52.3 | 63.1 | 52.3 | 63.1 |
底部产物17的组成[wt%] | ||||
500- | 0.12 | 0.32 | 0.08 | 0.23 |
500-540 | 0.59 | 1.86 | 0.42 | 1.53 |
540+ | 6.06 | 19.71 | 5.84 | 20.12 |
ASF-C5 | 54.96 | 46.42 | 55.39 | 46.45 |
THFis | 38.27 | 31.68 | 38.24 | 31.68 |
Q7,kg/h | 3220 | 2710 | 5216 | 4710 |
流7的组成[wt%] | ||||
H2O | 31.05 | 36.90 | 57.52 | 63.70 |
500- | 11.47 | 13.34 | 7.09 | 7.74 |
500-540 | 20.06 | 22.34 | 12.44 | 13.07 |
540+ | 36.44 | 27.35 | 22.63 | 15.48 |
ASF-C5 | 0.98 | 0.07 | 0.33 | 0.02 |
THFis | 0 | 0 | 0 | 0 |
从前面的实验例子,可以观察到本发明的方法极其有效和显著的将供料流1的轻质和挥发性馏分与重质和固体馏分分离,前者极其浓缩在流Q7中,后者浓缩在流Q17中。更具体的,在流Q7中,沥青质ASF-C5和软沥青540+的含量明显减少,并且固体THFi残留物几乎被消除;后者几乎完全限制到固体流Q17中。
还可以观察到通过降低分离器6中的压力P6,流Q17中的沥青质ASF-C5的百分比如何降低,和因此所述方法的分离和脱沥青效率。
数字实施例的结果
更普遍的,不管前面的数字实施例的具体条件如何,本发明的方法特别适于处理底部排污流1,基于烃的残留物或者其他有机残留物,其含有至少30重量%且高达超过45-50重量%的不溶于戊烷的沥青质和/或不溶于四氢呋喃的其他残留物。
无需借助于机械离心分离,本发明的方法可以使得所处理的流的温度远超150℃,这使得它们更流动和更易于在连续方法中处理(如前述实施方案那样),而非整体设备或者它的一些部件的批次处理。通常,本发明能够获得更有效的冲洗,并且还在极其简单的设备中启动所述方法,因为它装备了仅仅一个分离器6,即,仅仅一个分离塔。
另一方面,当所处理的流的温度基本上不超过450℃和通常不经历过度苛刻的条件时,在一方面,本发明的方法不降解或者基本上不损害待处理的残留物的较高挥发性组分,这增加了所萃取的量,和另一方面,避免了在同一设备中形成焦炭,降低了维护的必需性和增加了它的运行寿命。
依靠动力流体9(特别是通过文丘里管8)在第一分离器6中压力控制适于插入设备中连续起作用。
前述实施方案例子可以进行不同的改变和变化,全部包括在本发明的保护范围中。冷却的传送带18例如可以更通常的用其他冷却传送机或者载体代替。全部细节可以用技术上等价元件来代替。所用材料例如作为尺寸也可以根据技术要求而变化。应当注意的是表述例如“A包含B,C,D”还包含和描述了这样具体的例子,在其中“A由B,C,D组成”。本专利申请的实施例和可能的变量列举应当被认为是非限定性的列举。
Claims (17)
1.一种处理重质烃基残留物(1),特别是处理具有高沥青质含量的沥青残留物的方法,其包括下面的步骤:
-将待处理的重质残留物置于325-500℃的温度;
-在压力等于或者低于大约0.1bara和温度等于或者低于450℃的环境中,使该待处理的重质残留物经历基本上绝热膨胀,以从该待处理的重质残留物中分离:
-第一较低挥发性馏分(17),其在大气压下的沸点等于或者高于540℃,并且它的固体和/或无水残留物主要包含不溶于戊烷的沥青质和/或不溶于四氢呋喃的其他残留物;
-和第二较高挥发性馏分(7),其主要含有软沥青和在大气压下的沸点等于或者低于540℃的其他烃。
2.根据权利要求1的方法,其中具有高沥青质含量的沥青残留物包含20-45重量%量的C5-沥青质和10-20重量%量的THFis。
3.根据权利要求1或2的方法,其中待处理的重质残留物是从高于1bara的压力开始膨胀的。
4.根据权利要求3的方法,其中待处理的重质残留物是从1-2bara的压力开始膨胀的。
5.根据权利要求1或2的方法,其中绝热膨胀是基本上瞬时的。
6.根据权利要求1或2的方法,其包括通过将待处理的烃基残留物送过复合阀(8)来进行绝热膨胀的步骤。
7.根据权利要求1或2的方法,其中待处理的重质残留物(1)包含至少30重量%不溶于戊烷的沥青质和/或不溶于戊烷和/或四氢呋喃的其他残留物。
8.根据权利要求7的方法,其中待处理的重质残留物的C5-沥青质含量是20-45重量%且THFis含量是10-20重量%。
9.根据权利要求1或2的方法,其中第一较低挥发性馏分(17)的沥青质+THFis的含量是75-94重量%且软沥青和其他轻质烃的含量是6-25重量%。
10.根据权利要求1或2的方法,其包括如下步骤以获得待处理的重质残留物(1):将重质油转化成较低分子量物质,使重质油进行氢化裂解,可能在催化剂例如基于钼、镍、钴或者其他过渡金属的催化剂存在下进行。
11.根据权利要求10的方法,其中氢化裂解是通过将氢鼓泡到重质油物质或者其他烃基物质中来进行的。
12.根据权利要求1或2的方法,其包括通过将水蒸气或者其他气态物质流引入待处理的重质残留物(1)中来流化该待处理的重质残留物(1)的步骤。
13.根据权利要求12的方法,其中水蒸气或者其他气态物质与待处理的重质残留物的流量之比是以体积计0.03-0.75,更优选以体积计0.03-0.5。
14.根据权利要求1或2的方法,其包括在包含容器的分离器(6)中进行基本上绝热膨胀,和在所述容器的底部上收集非气态形式,例如处于液体、糊或者淤浆的形式,的第一较低挥发性馏分(17)的步骤。
15.根据权利要求1的方法,其包括在冷却的传送带(18)上沉积第一较低挥发性馏分(17)的步骤,所述冷却的传送带(18)的表面温度等于或低于100℃。
16.根据权利要求15的方法,其包括通过与冷却的传送带(18)接触而通过冷却将第一较低挥发性馏分(17)凝固和可能碎化成颗粒的步骤。
17.根据权利要求1或2的方法,特征在于它是连续方法。
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PCT/IT2013/000115 WO2014174536A1 (en) | 2013-04-22 | 2013-04-22 | Process for treating a hydrocarbon-based heavy residue |
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EP (1) | EP2989182B1 (zh) |
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CA (1) | CA2908439C (zh) |
ES (1) | ES2692947T3 (zh) |
PL (1) | PL2989182T3 (zh) |
PT (1) | PT2989182T (zh) |
RS (1) | RS57904B1 (zh) |
RU (1) | RU2634727C2 (zh) |
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CN105709445A (zh) * | 2016-02-19 | 2016-06-29 | 中石化炼化工程(集团)股份有限公司 | 含固油气的脱固方法 |
CN105833550A (zh) * | 2016-04-12 | 2016-08-10 | 中石化炼化工程(集团)股份有限公司 | 含固油气的脱固方法 |
CN106978209A (zh) * | 2016-01-19 | 2017-07-25 | 肇庆市顺鑫煤化工科技有限公司 | 一种煤直接液化产物的分离方法和装置 |
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IT201700035782A1 (it) * | 2017-03-31 | 2018-10-01 | Eni Spa | Metodo per la separazione fisica di correnti di spurgo da raffineria. |
ES2796092B2 (es) * | 2020-06-03 | 2021-07-05 | Cuetos Evaristo Fontecha | Sistema y procedimiento de extraccion selectiva de hidro-carburos viscosos de tanques y otros recipientes |
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CN105833550A (zh) * | 2016-04-12 | 2016-08-10 | 中石化炼化工程(集团)股份有限公司 | 含固油气的脱固方法 |
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US20160068760A1 (en) | 2016-03-10 |
WO2014174536A1 (en) | 2014-10-30 |
CA2908439C (en) | 2020-04-28 |
PL2989182T3 (pl) | 2019-01-31 |
EP2989182B1 (en) | 2018-08-01 |
RU2015144506A (ru) | 2017-05-26 |
TR201815716T4 (tr) | 2018-11-21 |
RS57904B1 (sr) | 2019-01-31 |
PT2989182T (pt) | 2018-11-14 |
CA2908439A1 (en) | 2014-10-30 |
RU2634727C2 (ru) | 2017-11-03 |
ES2692947T3 (es) | 2018-12-05 |
EP2989182A1 (en) | 2016-03-02 |
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