CN104114679A - 使用级间蒸汽汽提的加氢裂化方法 - Google Patents
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- 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
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
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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
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/301—Boiling range
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- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4093—Catalyst stripping
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Abstract
在加氢裂化方法中,使来自第一级反应器的产物通过蒸汽汽提塔以除去氢、H2S、NH3、轻质气体(C1-C4)、石脑油和柴油产物。使汽提塔塔底油从氢、H2S、NH3、轻质气体(C1-C4)、石脑油和柴油产物中分离并且在第二级反应器中处理。将来自第二级反应器的流出物物流,连同分离的氢、H2S、NH3、轻质气体(C1-C4)、石脑油和柴油产物的物流,传送至分离段用于分离石油馏分。优选地,在蒸汽汽提步骤之前使来自第一级反应器的流出物物流通过蒸汽发生器。在替代的实施方案中,在蒸汽汽提步骤之前,使来自第一级反应器的流出物物流通过蒸气/液体分离器汽提塔容器。
Description
相关申请的交叉引用
本申请要求2011年7月29日提交的美国临时专利申请号61/513,029的优先权,其内容以引用方式并入本文。
本发明背景技术
加氢裂化方法是公知的并且用于大量石油精炼厂。这样的方法伴随从石脑油到非常重质原油残余馏分的各种进料使用。一般,加氢裂化方法将进料分子分开成较小(较轻质)的具有更高的平均挥发性和经济价值的分子。同时,加氢裂化方法一般通过增加材料的氢:碳比例,并且通过除去硫和氮改进处理的材料的质量。加氢裂化方法的显著经济效用已经导致付出大量开发努力,用于改进该方法并且用于开发用于该方法的更好的催化剂。
加氢裂化单元由用于反应和分离的两个主要部分(principalsection)构成,其配置和类型是不同的。存在多种已知的工艺配置,包括直流(once-through)或串流、两级直流、使用循环的两级、单级和温和加氢裂化。参数(例如原料质量、产品规格、工艺目标和催化剂)确定反应部分的配置。
在直流配置中,使用两个反应器。原料在加氢处理催化剂之上在第一反应器中精炼并且将流出物送至包含(一种或多种)无定形或沸石基裂化催化剂的第二反应器。在两级配置中,在加氢处理催化剂之上在第一反应器中精炼原料并且将流出物送至分馏器塔以分离在36-370℃的标称范围中沸腾的H2S、NH3、轻质气体(C1-C4)、石脑油和柴油产物。然后将在370℃以上的温度下沸腾的烃循环至第一级反应器或第二反应器。
在两种配置中,将加氢裂化单元流出物送至蒸馏塔以分馏分别在36-180℃、180-240℃、240-370℃和370℃以上的标称范围中沸腾的石脑油、喷气/煤油、柴油和未转化的产物。加氢裂化产物喷气/煤油(即,发烟点>25mm)和柴油产物(即,十六烷值>52)是高质量并且很好地在世界范围的运输燃料规格以上的。
两级配置的一个优点是其最大化了中间馏出物收率。使来自第一级的转化的产物分馏并且不经受第二反应器中进一步的裂化,导致了高中间馏出物收率。
使用循环的现有技术常规两级加氢裂化单元图示性展示于图1中。在所示配置中,在第一反应器10中在加氢处理催化剂之上加氢裂化原料11,所述催化剂通常为包含Ni、Mo或Ni、W或Co、Mo金属作为活性相的无定形基催化剂。然后将第一反应器流出物物流12传送至分馏器20并且分离包含在高至370℃的标称温度沸腾的H2S、NH3、C1-C4气体、石脑油和柴油馏分的轻质馏分21。将在370℃以上沸腾的烃馏分22送至包含(一种或多种)无定形和/或沸石基催化剂的第二反应器30,所述催化剂包含Ni、Mo或Ni、W金属作为活性相。将第二反应器流出物物流31循环至分馏器20以形成物流13用于分离较轻质的裂化组分。
分离部分的配置取决于反应器流出物的组成。将反应器流出物送至热分离器或冷分离器。在后者的情况中,在通过进料/流出物交换器之后,将反应器流出物送至高压冷分离器。将部分未转化的循环物流作为排放(bleed)物流24从分馏器塔底油中取出。然后在压缩之后将气体循环回至反应器并且将塔底油送至低压低温分离器用于进一步的分离。
在热方案中,使反应器流出物通过交换器并且送至高压热分离器,气体从其循环至反应器。塔底油送至高压冷分离器并且至低压低温分离器用于进一步的分离。
通常设计利用冷分离器的加氢裂化单元用于处理从石脑油至柴油的较轻质的原料。设计利用热分离器的加氢裂化单元用于较重质的原料、减压粗柴油和较重质的组分。两种方案都存在优点和缺点。在利用热分离器的方案中进料/流出物换热器的表面积显著降低。不需要冷却全部流出物至40℃并且如在冷方案中地预加热汽提塔。因为热效率,该方案也导致了就进料预加热而言的热获得,其为的冷方案炉要求的约30-40%。热方案的缺点为循环气体与冷方案中所获得的相比一般更不纯,其导致了更高的反应器入口压力。使用热方案的氢消耗也略微更高,这是由于更高的氢溶解度。
单级直流加氢裂化是常规加氢裂化的更温和的形式。用于温和加氢裂化的操作条件比加氢处理方法更剧烈并且比常规高压加氢裂化方法更不剧烈。该方法为更成本高效的加氢裂化方法,但是导致了降低的产物收率和质量。温和加氢裂化方法相比于常规加氢裂化方法产生更少的相对较低质量的中间馏出物产物。可以使用单个或多个催化剂***并且其选择基于处理的原料和产品规格。热和冷工艺方案都可以用于温和加氢裂化,其取决于工艺要求。单级加氢裂化使用最简单的配置并且设计这些单元用于使用单或双催化剂***最大化中间馏出物收率。双催化剂***用于堆积床配置或用于两个串联反应器中。
可以以直流模式或以循环(具有未转化的进料至反应器的循环)模式操作单级加氢裂化单元。加氢处理反应在第一反应器中发生,其负载有无定形基催化剂。加氢裂化反应在第二反应器中在无定形基催化剂或沸石基催化剂之上发生。在串流配置中,将加氢处理的产物送至第二反应器。在循环至消失操作模式中,将来自第一级的反应器流出物与第二级流出物一起送至分馏器用于分离,并且将未转化的塔底油(不含H2S和NH3)送至第二级。也存在多种两级配置。
现有技术中已知使用蒸汽汽提以使轻质组分(例如C1-C4气体)和H2S及NH3分离。USP6,042,716公开了一种方法,其中粗柴油和氢在催化剂的存在下反应用于深度脱硫和深度脱氮。蒸汽汽提流出物以分离气相,并且通过在催化剂的存在下与氢的反应使液相脱芳构化。在给定的实例中,粗柴油在184-394℃的范围中沸腾,并且将蒸汽汽提用于从液相中分离气相。蒸汽汽提通常用于精炼操作以汽提烃气体甲烷、乙烷、丙烷和丁烷和含杂原子的气体,例如H2S和NH3。
在USP号5,164,070中,蒸汽用于除去轻质气体和石脑油。然而,分馏点为石脑油,其最终沸点为180℃。在所描述的方法中,蒸汽优选通过管线7加入至汽提塔底部以实施从进入液体中汽提较轻质的烃和较有挥发性的材料。替代地,可以将再沸器放置在汽提塔底部以实施或协助达到希望的汽提程度。汽提塔旨在从进入液体物流中除去大部分的石脑油沸点烃并且也旨在除去基本上全部较低沸点烃。通过管线8将剩余的较重质的烃作为净汽提塔塔底油物流排出。
USP5,4476,21公开了中间馏出物提质加工(upgrading)方法,其中蒸汽用于除去挥发性组分,但是不除去重质馏分,例如柴油,其是本专利中的原料。
USP5,453,177和USP6,436,279中公开的方法利用蒸汽汽提以除去轻馏分组分。
USP7,128,828公开了一种方法,其使用减压蒸汽汽提塔除去低沸点、非蜡馏出物烃塔顶馏出物。
USP7,279,090,将蒸汽汽提用于在集成了溶剂脱沥青和使在523℃和更高沸腾的减压渣油原料沸腾床渣油转化的方法中分离在36-523℃的范围中沸腾的烃馏分,并且将蒸汽汽提用于从在523℃和以下沸腾的其它馏分中分离渣油。
多个文献公开了在总加氢裂化单元内的多个加氢裂化区域的使用。本文中用作加氢裂化单元的术语“加氢裂化区域”通常包含多个个体应器。加氢裂化区域可以包含两个或更多个反应器。例如,USP3,240,694展示了加氢裂化方法,其中将进料物流进料至分馏塔中并且分成轻质馏分和重质馏分。使轻质馏分通过加氢处理区域并且然后传送至第一加氢裂化区域中。将重质馏分传送至第二、单独的加氢裂化区域中,伴随着在单独的分馏区域中将该加氢裂化区域的流出物分馏以产生轻质产物馏分、传送至第一加氢裂化区域的中间体馏分和循环至第二加氢裂化区域的塔底油馏分。
标题为“Process for the hydrocracking of a hydrocarbonaceousfeedstock”的USP4,950,384使用闪蒸器分离第一级反应器流出物。烃类原料通过如下加氢裂化:在第一反应级中在升高的温度和压力下在氢的存在下使原料与第一加氢裂化催化剂接触以获得第一流出物,在与第一反应级中普遍的(prevailing)温度和压力基本上相同的温度和压力下从第一流出物中分离气相和液相,在第二反应级中在升高的温度和压力下在氢的存在下使第一流出物的液相和第二加氢裂化催化剂接触以获得第二流出物,通过分馏从气相和第二流出物的组合中获得至少一种馏出物馏分和残余馏分,和将至少部分残余馏分循环至反应级。
USP6,270,654描述了利用具有级间分离的多级沸腾床反应器的催化加氢方法,通过在系列沸腾床反应器之间的闪蒸进行所述级间分离。该方法仅仅在520℃以上沸腾的残留原料上进行。
USP6,454,932描述了使用级间汽提和分离的多级沸腾床加氢裂化,其采用分离步骤,并且在沸腾床反应器之间使用氢汽提。该方法在650℃和以上沸腾的原料上进行,并且在减压馏出物和渣油两者上使用。
USP6,620,311公开了用于转化石油馏分的方法,其包括沸腾床加氢转化步骤、分离步骤、加氢脱硫步骤和利用蒸汽汽提塔的裂化步骤。
USP4,828,676和USP4,828,675公开了一种方法,其中使含硫进料加氢、汽提并且与氢在第二级中反应。将蒸汽汽提用于除去H2S(但是不是石脑油和柴油产物),如显示于col.10,1.11;col.11,1.7-10;col.25,1.18-22中的。
Gupta的USP6,632,350和USP6,632,622公开了使用在相同容器中的第一级流出物的汽提的两级容器。Gupta的美国专利6,103,104和5,705,052公开了使用在分离汽提塔容器中的第一级流出物的汽提的两级容器。Gupta的专利中公开的方法也使用蒸汽汽提除去液体中溶解的气体。
USP7,279,090使用了蒸汽汽提以分离在36-523℃的范围中沸腾的石脑油、柴油和VGO馏分。然而,该专利要求保护的是处理在523℃和更高沸腾的减压渣油原料的集成方法。
发明内容
本发明为用于加氢裂化烃原料的方法。将原料供应至第一级反应器的进料(input)中用于除去杂原子并且使高分子量分子裂化成低分子量烃。使来自第一级反应器出口的流出物物流通过蒸汽汽提塔容器以除去氢、H2S、NH3、轻质气体(C1-C4)、石脑油和柴油产物。将汽提塔塔底油单独于氢、H2S、NH3、轻质气体(C1-C4)、石脑油和柴油产物从汽提塔容器中除去并且供应至第二级反应器的进料。然后来自第二级反应器的出口的流出物物流,与氢、H2S、NH3、轻质气体(C1-C4)、石脑油和柴油产物的流出物物流(其已经从蒸汽汽提塔容器中除去)在一起供应至分离段用于分离石油馏分。
优选地,在供应至蒸汽汽提塔容器之前使来自第一级反应器的流出物物流通过蒸汽发生器。
替代地,在供应至蒸汽汽提塔容器之前使来自第一级反应器的流出物物流通过蒸气液体分离器汽提塔容器。
本发明将要通过将直流配置转化成两级配置改进加氢裂化工艺操作,特别是对于现有的单元。所提议的配置或改进将要改进加氢裂化单元工艺性能,产生更多希望的中间馏出物产物和更少的不希望的轻质气体C1-C4和石脑油并且如相比于现有工艺的,将要延长催化剂寿命。
通过在加氢裂化单元的第一和第二级之间安置蒸汽汽提步骤,很大地改进了工艺性能和收率。
因此,与利用闪蒸或蒸馏单元的已知现有技术***相反,本发明利用加氢裂化单元级之间的蒸汽汽提。
依据本发明的蒸汽汽提的使用产生简单就如下而言的解决方案:有效分离加氢裂化第一级流出物并且高效利用第二反应器体积。存在多个优点:轻质裂化产物(例如石脑油和中间馏出物)的最小化的裂化导致了高中间馏出物收率和较低的石脑油和C1-C4气体产量,通过除去H2S消除了其中毒效应并且在第二级反应器中保持了较高的催化剂活性。
相似地,将蒸汽汽提用于除去全部形成的轻质气体。
蒸汽汽提塔在两个加氢裂化级之间分离在375℃和以下沸腾的馏分,其中减压粗柴油在375-565℃的范围中沸腾。蒸汽汽提工艺步骤比闪蒸分离更有效并且可以并入至现有加氢裂化单元配置中,其中蒸汽发生器可以容易地安置。
附图说明
本发明将要在以下进一步详细地并且参照附图描述,所述附图中相同和相似的要素将要由相同数字代表,并且其中:
图1为现有技术的常规两级加氢裂化单元的示意图;
图2为本发明实施方案示意图;
图3为本发明另一个实施方案的示意图;和
图4为本发明进一步的实施方案的示意图。
具体实施方式
参照图2,将烃原料物流11和氢物流12进料至第一级反应器容器10用于除去杂原子(包含硫、氮)和痕量的例如Ni、V、Fe的金属,并且还用于将高分子量、高沸点分子裂化成5-60W%的较低分子量、较低沸点烃。
将流出物物流13送至蒸汽产生换热器20用于冷却反应产物并且用于从水21产生蒸汽22。将来自蒸汽发生器的冷却产物23送至蒸汽汽提塔容器30以除去在36-370℃的标称范围中沸腾的氢、H2S、NH3、轻质气体(C1-C4)、石脑油和柴油产物。给蒸汽汽提塔提供来自蒸汽发生器20的蒸汽22。
使汽提塔塔底油32(不含轻质气体、H2S、NH3和轻质馏分物流31)与氢物流33组合并且送至加氢裂化单元容器40的第二级。使第二级流出物物流41与轻质汽提塔产物31组合,并且将组合的物流42送至多个分离和清洗容器(包括分馏器容器50)以获得最终加氢裂化气体和液体产物。
加氢裂化器产物包括物流51(其包含H2S、NH3、轻质气体(C1-C4))、在C5-180℃的范围中沸腾的石脑油物流52、在180-240℃的范围中沸腾的煤油物流53、在240-370℃的范围中沸腾的柴油物流54和在370℃以上沸腾的未转化的烃馏分物流55。
现在参照图3的实施方案,将烃原料物流11和氢物流12进料至第一级反应器容器10用于除去杂原子(包含硫,氮)和痕量的例如Ni、V和Fe的金属,并且也用于将高分子量、高沸点分子裂化成5-60W%的较低分子量、较低沸点烃。将流出物物流13送至换热器蒸汽发生器20以冷却反应产物并且从进料水21产生蒸汽22。将来自蒸汽发生器的冷却产物23送至蒸气/液体分离器汽提塔30以除去轻质气体(包括氢、H2S、NH3和C1-C4烃),其作为流出物物流31离开。
将蒸气/液体分离器塔底油物流32送至蒸汽汽提塔容器40以除去通常在36-370℃的范围中沸腾的石脑油和柴油产物。通过由蒸汽发生器20产生的蒸汽22给蒸汽汽提塔进料。使汽提塔塔底油42(不含轻质气体、H2S、NH3和轻质馏分)与氢物流43组合并且送至第二级加氢裂化单元容器50。
然后使第二级流出物物流51与轻质汽提塔产物41组合,并且将组合的物流52送至多个分离和清洗容器(包括分馏器容器60)以获得最终加氢裂化气体和液体产物。加氢裂化器产物包括H2S、NH3、轻质气体(C1-C4)物流61、在36-180℃的范围中沸腾的石脑油物流62、煤油物流63、在180-370℃的范围中沸腾的柴油物流64和在370℃以上沸腾的未转化的烃馏分物流65。
图4中显示的实施方案包括与图2的实施方案相似的单元操作进行方法。然而,此外,图4实施方案包括用于加氢处理柴油物流和水循环物流的柴油加氢处理器。如图4中所示,使部分汽提塔塔顶物流31通过蒸汽发生器至分离器容器60以分离水、气体和液体。提取部分水并且送回至蒸汽发生器20并且其后至汽提塔单元30。
将来自精炼厂的含硫柴油物流供应至容器60,与塔顶物流组合,并且送至柴油加氢处理器70,用于超低硫柴油的生产。将来自加氢处理器单元70的剩余的水循环至汽提塔单元30,同时回收来自加氢处理器的超低硫或脱硫(sweet)柴油(“ULSD”)用于市场。
实施例
包含15V%的脱金属油(DMO)和85V%的减压粗柴油(VGO,其64%为重质VGO并且21%为轻质VGO)的原料共混物在由Ni、W、Mo金属促进的无定形和沸石载体构成的催化***之上,在115kg/cm2的氢分压、每小时1000m3的催化剂之上800m3的原料、1,265升氢:油比例和370-385℃的温度下经受加氢裂化,所述共混物的特性显示于表1中。
表1
特性 | 单位 | 方法 | 共混物 |
比重 | 0.918 | ||
API比重 | ° | ASTM D4052 | 22.6 |
硫 | W% | ASTM D5453 | 2.2 |
氮 | ppmw | ASTM D5762 | 751 |
溴数 | g/100g | 3.0 | |
氢 | W% | ASTM D4808 | 12.02 |
模拟的蒸馏 | ASTM D7213 | ||
IBP | ℃ | 210 | |
10/30 | ℃ | 344/411 | |
50/70 | ℃ | 451/498 | |
90/95 | ℃ | 590/655 | |
98 | ℃ | 719 |
产物收率显示于表2中。第一级流出物的蒸汽汽提使中间馏出物收率改进了约5W%并且将产生的石脑油和轻质气体分别降低了约5W%和0.5W%。
表2
直流 | 使用级间汽提的直流 | |
H2S,W% | 2.58 | 2.58 |
C1-C4,W% | 3.21 | 2.85 |
石脑油,W% | 25.16 | 19.77 |
中间馏出物,W% | 42.11 | 47.86 |
塔底油,W% | 29.60 | 29.60 |
总共,W% | 102.65 | 102.65 |
本发明利用蒸汽汽提塔以通过从第一级流出物中除去通常在36-370℃的范围中沸腾的H2S、NH3、轻质气体(C1-C4)、石脑油和柴油产物模拟两级加氢裂化单元配置。蒸汽-汽提产物将不含H2S和NH3并且将要包含未转化的烃,导致就催化剂而言的较高活性,因为不存在有毒的H2S和NH3,并且导致较高的中间馏出物选择性,因为轻质产物将不经受进一步的裂化。
尽管已经在多个实施方案中详细描述并且在图中展示了本发明,其它修改对本领域技术人员来说将是从说明书中显而易见的,并且本发明的范围将由以下的权利要求书确定。
Claims (10)
1.用于加氢裂化烃原料的方法,其包括如下步骤:
将原料供应至第一级反应器的进料用于除去杂原子并且将高分子量分子裂化成较低分子量烃,以产生第一级反应器流出物;其后
将第一级流出物传送至蒸汽汽提塔容器以分离氢、H2S、NH3、轻质气体(C1-C4)、石脑油和柴油产物;
将汽提塔塔底油从汽提塔容器传送至第二级反应器;
使第二级反应器的加氢裂化流出物物流与蒸汽汽提塔容器中分离的氢、H2S、NH3、轻质气体(C1-C4)、石脑油和柴油产物组合以形成组合的产物物流;并且将组合的产物物流传送至分离段用于将组分分离成预定的产物物流。
2.根据权利要求1的方法,其中在传送至蒸汽汽提塔容器之前,使来自第一级反应器的流出物物流通过换热蒸汽发生器。
3.根据权利要求1的方法,其中在传送至蒸汽汽提塔容器之前,使来自第一级反应器的流出物物流通过蒸气/液体分离器汽提塔容器。
4.根据权利要求1的方法,其中第一级加氢裂化催化剂选自无定形氧化铝催化剂、无定形二氧化硅氧化铝催化剂、沸石基催化剂,以及包含无定形氧化铝催化剂、无定形二氧化硅氧化铝催化剂和沸石基催化剂的至少一者的组合。
5.根据权利要求1的方法,其中第一级加氢裂化催化剂进一步包含Ni、W、Mo、Co,或包含Ni、W、Mo和Co的至少一者的组合的活性相。
6.根据权利要求1的方法,其中以体积计10%-80%的在370℃以上在100-200kg/cm2的氢分压下沸腾的烃转化成一种或多种轻质气体,所述轻质气体选自甲烷、乙烷、丙烷、正丁烷、异丁烯、硫化氢、氨、在180℃-375℃的范围中沸腾的石脑油馏分、在180℃-375℃的范围中沸腾的柴油馏分,以及包含上述的轻质气体的至少一者的组合。
7.根据权利要求1的方法,其中氢分压为100-150kg/cm2。
8.根据权利要求1的方法,其中原料油的流量为每小时1000m3加氢处理催化剂之上300-2000m3。
9.根据权利要求1的方法,其中反应器为固定床、沸腾床、淤浆床或其组合。
10.根据权利要求1的方法,其中将从蒸汽汽提塔容器中除去的氢、H2S、NH3、轻质气体(C1-C4)、石脑油和柴油产物的部分流出物物流导向通过分离器容器以分离水、气体和液体;也将含硫柴油物流供应至分离器容器以与流出物物流混合;并且其中将组合的流出物物流/含硫柴油物流导向通过柴油加氢处理器单元以产生超低硫柴油燃料。
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EP (1) | EP2737027B1 (zh) |
JP (1) | JP6273202B2 (zh) |
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CN104114679B (zh) | 2016-04-13 |
WO2013019624A1 (en) | 2013-02-07 |
KR20140079763A (ko) | 2014-06-27 |
JP6273202B2 (ja) | 2018-01-31 |
EP2737027A1 (en) | 2014-06-04 |
US20130098802A1 (en) | 2013-04-25 |
JP2014527100A (ja) | 2014-10-09 |
WO2013019624A9 (en) | 2013-09-19 |
KR101956407B1 (ko) | 2019-03-08 |
EP2737027B1 (en) | 2018-12-26 |
US9803148B2 (en) | 2017-10-31 |
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