CN104011181B - 具有集成中间氢分离和纯化的加氢处理和芳烃饱和方法 - Google Patents
具有集成中间氢分离和纯化的加氢处理和芳烃饱和方法 Download PDFInfo
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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
- 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
- C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
- C10G65/08—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a hydrogenation of the aromatic hydrocarbons
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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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/44—Hydrogenation of the aromatic hydrocarbons
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- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
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- 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
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- 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
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- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
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Abstract
中间氢分离和纯化***与加氢处理和芳烃饱和方法集成,用于从包含含硫和含芳烃的烃化合物的相对重质原料生产相对低分子量的产品。该集成方法允许在单级配置中处理具有高芳烃和高硫含量的重质烃原料以及在芳烃饱和区中使用贵金属催化剂。该集成方法增加了整体的催化活性和加氢能力以生产优质馏出物产品。
Description
相关申请
本申请要求于2011年11月4日提交的美国临时专利申请61/555,905的权益,其披露的内容通过引用结合于此。
发明背景
技术领域
本发明涉及加氢处理和芳烃饱和***和方法,用于在现有的或者新的加氢裂化设施中从高硫高芳烃有效生产高品质馏出物。
相关技术描述
加氢处理技术是公知的现有技术,其中在200℃-500℃(392°F-932°F)范围内的温度和34barg-100barg(493ps ig-1450psig)范围内的压力,将在150℃-400℃(302°F-752°F)范围内沸腾的烃原料与氢混合,并使混合物经过非均相固定床催化剂。烃原料中的杂质,如硫、氮和氧化合物几乎完全被除去,并且任何存在的烯烃都得到饱和,从而产生基本上纯的链烷烃和环烷烃的混合物产品。一些芳烃成分也得到饱和。可接受的产品将满足超低硫馏出物的规格。非均相固定床催化剂含有至少一种第VIII族金属和至少一种第VIB族金属。通常,这些金属包含在载体材料如含或不含二氧化硅或某种其他促进剂的氧化铝上。
当在升高的氢压力和温度下在催化剂的固定床上处理进料时,发生所需程度的加氢处理。通过进料和所需产品的品质来设定所需催化剂量/进料体积和压力水平。
当需要最大程度的芳烃饱和时,将馏出物加氢处理段的产品随后进一步在芳烃饱和反应区加以处理。馏出物的芳烃饱和也是公知的现有技术,其中在200℃-400℃(392°F-752°F)范围内的温度和34barg-100barg(493psig-1450psig)范围内的压力,再次使烃原料与氢混合,并使混合物经过非均相固定床催化剂。非均相固定床催化剂含有至少一种第VIII族贵金属。通常,这些金属包含在载体材料如含或不含酸性裂化组分的氧化铝,如无定形氧化硅-氧化铝或沸石上。烃原料转化为高价值的低硫、低芳烃产品,其用作运输燃料并满足当前的超低硫馏出物的规格。
在升高的氢压力和温度下在催化剂的固定床上处理基本无硫的进料时,发生所需程度的芳烃饱和。通过进料和所需产品的品质来设定所需催化剂量/进料体积和压力水平。
当这些过程被组合成单一的单元时,传统的加氢处理后芳烃饱和在多个阶段中进行,或者在两个独立的单元中进行。随着烃进料中给定馏程的硫和芳烃含量增加,存在于加氢处理区流出物中的氨和硫化氢的量也将增加。硫化氢将开始抑制芳烃饱和,因此为了满足特定馏分高的十六烷值或发烟点,需要进一步处理。通过在第二阶段-芳烃饱和区增加氢化功能来催化地实现这一点。由于更高程度的氢化需要使用会受硫化氢毒化的贵金属催化剂,因此需要中间分馏段以汽提出硫化氢、氢和轻馏分。然后在脱硫的(不含硫化氢)第二阶段处理经汽提的进料,其中在贵金属催化剂体系上进行芳烃饱和,之后在分馏段汽提出硫化氢和轻馏分。这使整个设备的设计复杂化并增加了达到预期目标所需的循环气的量。
因此,在本领域中需要改进的加氢处理和芳烃饱和方法,特别是用于能够处理具有相对高的硫和芳烃含量的原料的新***,或者用于已经受到催化剂活性和馏出物选择性所限制的现有***。
发明概述
上述目的和进一步的优点通过此处所述的方法来提供。将中间氢分离和纯化***与加氢处理和芳烃饱和方法集成,用于从包含含硫和含芳烃的烃化合物的相对重质原料生产相对低分子量的产品。该集成方法允许在单级配置中处理具有高芳烃和高硫含量的重质烃原料以及在芳烃饱和区中使用贵金属催化剂。该集成方法增加了整体的催化活性和加氢能力以生产优质馏出物产品。
集成加氢处理方法用于从包含含硫和含芳烃的烃化合物的相对重质原料生产相对低分子量的产品。该方法包括:
a.在氢的存在下,用加氢处理催化剂对原料加氢处理,以产生含有减少量的含硫烃化合物的加氢处理流出物;
b.在高压分离区分离该加氢处理流出物以产生蒸气流和烃液体流;
c.在来自步骤(b)的蒸气流的至少一部分相对较重的组分的存在下,在吸收区纯化至少一部分该蒸气流,以产生高纯度氢气流和燃料气流;
d.在氢气的存在下,用芳烃饱和催化剂使部分该烃液体流中所含的芳烃化合物饱和,以产生芳烃饱和流出物,其中该氢气包括来自步骤(c)的该高纯度氢气流以及补充氢气流;以及
e.分离和分馏该芳烃饱和流出物,以产生一个或多个顶部气体流、一个或多个酸性水流以及顶部和底部分馏的馏出物产品。
在某些实施方式中,步骤(b)包括在热高压分离区分离该加氢处理流出物以产生加氢处理气体流和加氢处理液体流,以及在冷高压分离区分离该加氢处理气体流以产生蒸气流、烃液体流和酸性水流,其中步骤(c)中使用的该蒸气流的相对较重的组分来自由冷分离器产生的该蒸气流中的较重馏分的进一步冷凝和由冷高压分离区的部分该烃液体流提供的额外补充。
附图说明
在结合附图阅读时,以下详细描述将被最好地理解。出于说明本发明的目的,附图实施方案示出的是本发明优选的实施方式。然而应当理解,本发明并不限于所示的精确布置和装置。在附图中,相同的附图标记用来指代相同或相似的元件,其中:
图1是集成有中间氢分离和纯化***的加氢处理和芳烃饱和***的工艺流程图;以及
图2是吸收区的示意图。
发明详述
提供了集成加氢处理和芳烃饱和配置,其合并了氢分离区以及利用吸收来纯化氢。这些附加的步骤位于加氢处理反应区和芳烃饱和区之间。这从中间反应流出物中除去氨和硫化氢,并允许纯化氢流与待饱和的液体流在基本上无氨和无硫化氢的环境中重新合并。
特别地,现在参照图1,示出了集成加氢装置1000的工艺流程图。装置1000包括加氢处理区100、第一高压分离区200、芳烃饱和区300、吸收区400、第二高压分离区500、闪蒸区600和分馏区700。
加氢处理区100包括包含有效量的合适的加氢处理催化剂的反应器144。反应器144包括用于接收包括进料流120和氢流124的合并流130的入口以及用于接收急冷氢流146的入口。加氢处理流出物流140从反应器144的出口排出。在某些实施方式中,氢气入口可以与进料口(除了用于引入急冷氢的入口外)分开。
第一高压分离区200通常包括热高压分离容器210和冷高压分离容器220。热高压分离容器210包括用于接收加氢处理流出物140的入口,用于排放加氢处理气体流230的出口以及用于排出加氢处理液体流240的出口。包含选自包括氢、甲烷、乙烷、氨、硫化氢、C5+烃的组中的一种或多种气体的流230离开第一分离容器210。
冷高压分离容器220包括与分离容器210流体连通并用于接收部分冷凝的加氢处理气体流230的入口,用于排出蒸气流250的出口,用于排出酸性水流290的出口和用于排出烃液体流261的出口。在进入随后的冷高压分离器之前用于冷却热流所需的热交换器并未示出,本领域的普通技术人员应当能够理解对于热交换器的需求。
如图2所示,吸收区400包括交叉热交换器410、冷却器420、甲烷吸收塔430、闪蒸再生容器440和溶剂循环泵442。甲烷吸收塔430包括用于接收来自高压分离区200并经过交叉热交换器410和冷却器420后的蒸气流250的入口,用于接收来自闪蒸再生容器440的循环溶剂流444的入口,用于接收溶剂补充流260的入口,用于排出富溶剂液体流432的出口和用于排出氢流450的出口。在吸收区400,来自冷高压分离器220的相对低H2纯度的流250与来自在甲烷吸收塔430中作为溶剂的流260的冷凝烃液体的一部分逆流接触,以吸收甲烷和较重质烃,与所含的氢分离。流250在热交换器410中通过与更冷的、纯化的、回收的氢流450交叉换热而冷却,随后在制冷单元420中被冷却到约-20°F。在吸收塔430中,多数重质气体(包括甲烷、乙烷、丙烷、丁烷、戊烷)和较重质气体被吸收并与流250中所含的氢分离。来自吸收区430底部的富溶剂液体流432被送到至少一个闪蒸阶段440。通过在闪蒸罐中降低压力,分离富溶剂流432并得到贫液体溶剂流444,利用溶剂循环泵442可以将贫液体溶剂流444循环返回到甲烷吸收塔430。大部分用于吸收的溶剂主要是从冷却后的流250中冷凝得到的较重质烃类。烃流260主要用作补充溶剂。
与吸收区400相似的布置示于美国专利6,740,226、4,740,222、4,832,718、5,462,583、5,546,764和5,551,972,以及美国公布2007/0017851中,其披露的内容均通过引用整体结合于此。
根据描述,附图中的工艺流线可以指流、进料、产品或流出物。根据氨含量,可将水流(未示出)添加到流230以除去二硫化铵盐。流290主要是酸性水,可以将其送至任何合适的目的地如酸性水汽提塔。从分离器220分离的蒸气通过流250离开并进入吸收区400。将来自分离器220的液体烃排出流261的一部分260导向,如上所述,通过溶剂补充流260形成吸收溶剂用于吸收区400。作为来自分离器220的未导向为吸收溶剂补充260的流261的其余部分的烃流265,绕过芳烃饱和区300。
吸收区400通过用包含溶剂补充流260的循环溶剂吸收比氢重的组分来纯化存在于流250中的氢,以产生高纯度(95-99mol%)氢流450和包含存在于流250中比氢重的组分的燃料气体流460。
之后,高纯度氢流450与来自歧管“集管B”的高纯度补充氢流204同液体流240合并,形成进入芳烃饱和区300的合并进料330。
芳烃饱和区300包括芳烃饱和反应器320,其可具有一个或多个催化剂床层并接收由流326简单表示的床之间的急冷氢流,虽然只示出了一个急冷氢流,但应当理解,可根据床的数量向芳烃饱和反应器320提供多个流。芳烃饱和区300可以在任何合适的条件操作。来自芳烃饱和区300的流出物流340与来自分离器220的额外的烃流265合并,形成进入第二分离区500的流390。
分离区500包括分离容器510。在进入高压分离容器510之前,需要热交换器来冷却热流340。高压分离器罐510可提供包含氢和甲烷的塔顶流514(主要富含氢),进入闪蒸区600的烃流530和主要是酸性水的重质液体流520,酸性水可被送至任何合适的目的地如酸性水汽提塔。可将水流(未示出)添加到合并流390以除去铵盐。
闪蒸区600包括冷低压闪蒸罐610。冷却热流所需的热交换器并未示出,本领域的普通技术人员应当理解对其的需求。通常,闪蒸罐610通过压力降低来从冷凝液体或从液体中分离气体。
低压冷闪蒸罐610提供包含氢和甲烷的塔顶流614(主要富含氢),烃侧线馏分618和主要是酸性水的塔底流620,酸性水可被送至任何合适的目的地如酸性水汽提塔。烃液体侧线馏分618被引入分馏区700。
一般情况下,分馏区700生产各种产品,包括塔顶流710和塔底流750。通常,流710包含不稳定的石脑油,并且塔底流750基本上是高品质的馏出物产品,其在某些实施例中满足所需的产品品质标准如高十六烷值、高烟点和低硫含量。
高压分离罐510提供塔顶物流514,其富含氢并且可通过循环氢压缩机680压缩后循环回收以生成流685,流685被循环回氢歧管“集管A”。来自歧管“集管B”的高纯度补充氢流204通常可来自于氢生成单元。
用于本发明方法和装置的原料通常包含在150℃-400℃(302°F-752°F)沸腾的组分。通常,这些进料可以包括直馏粗柴油;原油蒸馏装置产品,如轻质减压粗柴油;减压蒸馏装置产品;热裂化粗柴油;减粘裂化装置、热裂化或焦化装置产品;轻质或重质循环油;流体催化裂化装置产品以及源自焦油砂的轻粗柴油。
一般情况下,加氢处理反应区可以包括加氢处理反应器,其可具有一个或多个催化剂床,并可接收床之间的急冷氢流。虽然只示出了一个氢急冷入口,但应当理解的是,可以在沿加氢处理反应器的任何地方提供氢流并可根据床的数量提供多个氢流。加氢处理反应器床层通常包含具有至少一种第VIII族金属和至少一种第VIB族金属的催化剂。第VIII族金属选自由铁、钴和镍组成的组。第VIB族金属选自由钼和钨组成的组。第VIII族金属的存在量可以为约2-20重量%,并且第VIB族金属的存在量可以为约1-25重量%。通常,这些金属包含在载体材料如二氧化硅或氧化铝上。加氢处理反应区的操作条件包括200℃至500℃(392°F至932°F)的反应温度,34barg至100barg(493psig至1450psig)的反应压力。
热高压分离区的操作条件包括200℃至500℃(392°F至932°F)的温度,和30barg至100barg(435psig至1450psig)的压力。冷高压分离区的操作条件包括60℃至250℃(140°F至482°F)的温度,和30barg至100barg(435psig至1450ps ig)的压力。
一般情况下,芳烃饱和区可包括芳烃饱和反应器,其可具有一个或多个催化剂床,并可接收床之间的急冷氢流。虽然只示出了一个氢急冷入口,但应当理解的是,可以在沿芳烃饱和反应器的任何地方提供氢流并可根据床的数量提供多个氢流。芳烃饱和反应器床通常包含具有至少一种第VIII族贵金属的催化剂。第VIII族贵金属选自包括铂、钯、钌、铑、锇和铱的组。通常,这些金属包含在载体材料如带有酸性组分的二氧化硅或氧化铝如无定形二氧化硅-氧化铝或沸石上。通常,第VIII族贵金属的存在量可以为约0.2-5重量%。芳烃饱和区的操作条件包括200℃至400℃(392°F至752°F)的反应温度,和30barg至100barg(435psig至1450psig)的反应压力。
分离区500的操作条件包括40℃至80℃(104°F至176°F)的温度,和30barg至100barg(435psig至1450psig)的压力。
冷低压闪蒸罐的操作条件包括40℃至80℃(104°F至176°F)的温度,和20barg至50barg(290psig至725psig)的压力。
分馏区的操作条件包括40℃至400℃(104°F至752°F)的温度,和0.05bar至20bar(0.73psig至290psig)的压力。
传热设备、流体输送设备和传质设备并未总是示出,本领域的普通技术人员应当理解对于这些设备的需求。
与传统的加氢处理配置相比,本文描述的集成加氢处理装置和方法提供了显著的优点。该集成方法允许在单级配置中处理具有高硫和高芳烃含量的重质烃进料,与使用两级设计的常规流程所需的正常气体流相比,能够使循环气量减少20体积%至30体积%。当处理高硫和高芳烃馏出物范围的原料时,该集成方法也不仅能够制造超低硫馏出物(ULSD),还能制造高烟点煤油和高十六烷值柴油。此外,由于可获得高纯度氢而在加氢处理区产生较高的氢分压,该集成方法允许降低***压力,从而节约建设成本。
已经在上文和附图中描述了本发明的方法和***;然而,对于本领域的普通技术人员而言修改将是清楚的,并且本发明的保护范围由所附权利要求书来限定。
Claims (7)
1.集成加氢处理方法,用于从包含含硫和含芳烃的烃化合物的相对重质原料生产相对低分子量的产品,该方法包括:
a.在氢的存在下,用加氢处理催化剂对原料加氢处理,以产生含有减少量的含硫烃化合物的加氢处理流出物;
b.在高压分离区分离该加氢处理流出物以产生蒸气流和烃液体流;
c.通过使该蒸气流的至少一部分与作为溶剂的冷凝的烃液体接触,以吸收甲烷和重质烃,并由此产生高纯度氢气流和燃料气流,从而在吸收区中纯化该蒸气流的至少所述部分,所述冷凝的烃液体来源于来自步骤(b)的该蒸气流的至少一部分相对重质组分;
d.在氢气的存在下,用芳烃饱和催化剂使部分该烃液体流中所含的芳烃化合物饱和,以产生芳烃饱和流出物,其中该氢气包括来自步骤(c)的该高纯度氢气流以及补充氢气流;以及
e.分离和分馏该芳烃饱和流出物,以产生一个或多个塔顶气体流、一个或多个酸性水流以及塔顶和塔底分馏的馏出物产品。
2.如权利要求1所述的方法,其中步骤(b)包括在热高压分离区分离该加氢处理流出物以产生加氢处理气体流和加氢处理液体流,以及在冷高压分离区分离该加氢处理气体流以产生蒸气流、烃液体流和酸性水流,其中步骤(c)中使用的该蒸气流的相对重质的组分来自由冷分离器产生的该蒸气流中的重质馏分的进一步冷凝和由来自冷高压分离区的部分该烃液体流提供的额外补充。
3.如权利要求2所述的方法,其中步骤(d)包括使来自热高压分离区的该加氢处理液体流中所含的芳烃化合物饱和。
4.如权利要求3所述的方法,其中步骤(e)包括
将该芳烃饱和流出物分离成塔顶气体流、冷凝烃液体流和酸性水流;
闪蒸该冷凝烃液体流以产生塔顶气体流、烃液体侧线流和酸性水流;
分馏该烃液体侧线流以产生分馏塔顶流和分馏塔底流;以及
将该分馏塔顶流和该分馏塔底流作为产品回收。
5.集成加氢处理方法,用于从包含含硫和含芳烃的烃化合物的相对重质原料生产相对低分子量的产品,该方法包括:
a.在氢的存在下,用加氢处理催化剂对原料加氢处理,以产生含有减少量的含硫烃化合物的加氢处理流出物;
b.在高压分离区分离该加氢处理流出物以产生蒸气流和烃液体流;
c.通过使该蒸气流的至少一部分与作为溶剂的冷凝的烃液体接触,以吸收甲烷和重质烃,并由此产生高纯度氢气流和燃料气流,从而在吸收区中纯化该蒸气流的至少所述部分,所述冷凝的烃液体来源于来自步骤(b)的该蒸气流的至少一部分相对重质组分;
d.在氢气的存在下,用芳烃饱和催化剂使部分该烃液体流中所含的芳烃化合物饱和,以产生芳烃饱和流出物,其中该氢气包括来自步骤(c)的该高纯度氢气流以及补充氢气流;
e.将该芳烃饱和流出物分离成塔顶气体流、冷凝烃液体流和酸性水流;
f.闪蒸该冷凝烃液体流以产生塔顶气体流、烃液体侧线流和酸性水流;以及
g.分馏该烃液体侧线流以产生分馏塔顶流和分馏塔底流。
6.如权利要求5所述的方法,其中步骤(b)包括在热高压分离区分离该加氢处理流出物以产生加氢处理气体流和加氢处理液体流,以及在冷高压分离区分离该加氢处理气体流以产生蒸气流、烃液体流和酸性水流,其中步骤(c)中使用的该蒸气流的相对重质的组分来自由冷分离器产生的该蒸气流中的重质馏分的进一步冷凝和由来自冷高压分离区的部分该烃液体流提供的额外补充。
7.如权利要求6所述的方法,其中步骤(d)包括使来自热高压分离区的该加氢处理液体流中所含的芳烃化合物饱和。
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Publication number | Priority date | Publication date | Assignee | Title |
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US9084945B2 (en) | 2013-08-19 | 2015-07-21 | Uop Llc | Enhanced hydrogen recovery |
US9303220B2 (en) | 2013-08-30 | 2016-04-05 | Uop Llc | Process and apparatus for producing diesel with high cetane |
US9359564B2 (en) | 2013-08-30 | 2016-06-07 | Uop Llc | Process and apparatus for producing diesel with high cetane |
CN105709806B (zh) * | 2014-12-04 | 2018-02-09 | 中国石油化工股份有限公司 | 一种viii族金属均匀分散的加氢裂化催化剂及其制备方法 |
US10428283B2 (en) | 2015-07-08 | 2019-10-01 | Uop Llc | Reactor with stripping zone |
US10301560B2 (en) | 2016-06-15 | 2019-05-28 | Uop Llc | Process and apparatus for hydrocracking a hydrocarbon stream in two stages with aromatic saturation |
CN106957681A (zh) * | 2017-03-31 | 2017-07-18 | 北京中科诚毅科技发展有限公司 | 一种提高加氢反应体系氢分压的方法及其设计方法和用途 |
US11253816B2 (en) * | 2019-05-10 | 2022-02-22 | Saudi Arabian Oil Company | Direct oxidation of hydrogen sulfide in a hydroprocessing recycle gas stream with hydrogen purification |
SA121430164B1 (ar) | 2020-09-21 | 2024-01-18 | انديان اويل كوربوريشن ليمتد | عملية ونظام لإنتاج مذيبات منزوعة العطريات متعددة الدرجات من تيارات الهيدروكربون |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5114562A (en) * | 1990-08-03 | 1992-05-19 | Uop | Two-stage hydrodesulfurization and hydrogenation process for distillate hydrocarbons |
EP1063275A1 (fr) * | 1999-06-25 | 2000-12-27 | Institut Francais Du Petrole | Procédé d'hydrotraitement d'un distillat moyen dans deux zones comprenant une zone intermédiaire de stripage |
US7384540B2 (en) * | 2001-11-22 | 2008-06-10 | Institut Francais Du Petrole | Two-step method for middle distillate hydrotreatment comprising two hydrogen recycling loops |
CN100558446C (zh) * | 2005-01-21 | 2009-11-11 | 埃克森美孚研究工程公司 | 改进氢处理的馏出物两段加氢处理 |
Family Cites Families (21)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4832718A (en) | 1982-05-03 | 1989-05-23 | Advanced Extraction Technologies, Inc. | Processing nitrogen-rich, hydrogen-rich, and olefin-rich gases with physical solvents |
US4740222A (en) | 1982-05-03 | 1988-04-26 | Advanced Extraction Technologies, Inc. | Recovery and purification of hydrogen from refinery and petrochemical off-gas streams |
US5110444A (en) | 1990-08-03 | 1992-05-05 | Uop | Multi-stage hydrodesulfurization and hydrogenation process for distillate hydrocarbons |
US5462583A (en) | 1994-03-04 | 1995-10-31 | Advanced Extraction Technologies, Inc. | Absorption process without external solvent |
US5546764A (en) | 1995-03-03 | 1996-08-20 | Advanced Extraction Technologies, Inc. | Absorption process for recovering ethylene and hydrogen from refinery and petrochemical plant off-gases |
CA2243267C (en) | 1997-09-26 | 2003-12-30 | Exxon Research And Engineering Company | Countercurrent reactor with interstage stripping of nh3 and h2s in gas/liquid contacting zones |
US6017443A (en) | 1998-02-05 | 2000-01-25 | Mobil Oil Corporation | Hydroprocessing process having staged reaction zones |
US6569314B1 (en) | 1998-12-07 | 2003-05-27 | Exxonmobil Research And Engineering Company | Countercurrent hydroprocessing with trickle bed processing of vapor product stream |
CN1119395C (zh) * | 1999-03-19 | 2003-08-27 | 中国石油化工集团公司 | 一种馏分油两段加氢脱芳烃的方法 |
FR2818283B1 (fr) | 2000-12-20 | 2003-02-14 | Inst Francais Du Petrole | Procede de traitement d'une charge hydrocarbonee comprenant une etape d'hydrotraitement en lit fixe a contre-courant |
US7166209B2 (en) | 2001-03-01 | 2007-01-23 | Intevep, S.A. | Hydroprocessing process |
US6447673B1 (en) | 2001-03-12 | 2002-09-10 | Fina Technology, Inc. | Hydrofining process |
US6740226B2 (en) | 2002-01-16 | 2004-05-25 | Saudi Arabian Oil Company | Process for increasing hydrogen partial pressure in hydroprocessing processes |
AU2002303230A1 (en) | 2002-04-03 | 2003-10-20 | Fluor Corporation | Combined hydrotreating and process |
US7238275B2 (en) | 2002-04-05 | 2007-07-03 | Fluor Technologies Corporation | Combined hydrotreating process and configurations for same |
US7247235B2 (en) * | 2003-05-30 | 2007-07-24 | Abb Lummus Global Inc, | Hydrogenation of middle distillate using a counter-current reactor |
CN1219033C (zh) * | 2003-05-31 | 2005-09-14 | 中国石油化工股份有限公司 | 一种馏分油加氢脱硫脱芳烃的方法 |
US20050035026A1 (en) | 2003-08-14 | 2005-02-17 | Conocophillips Company | Catalytic distillation hydroprocessing |
MX2007008394A (es) | 2005-01-21 | 2007-09-07 | Exxonmobil Res & Eng Co | Hidrotratamiento de dos etapas de destilados con manejo de hidrogeno mejorado. |
MX2007008431A (es) | 2005-01-21 | 2007-09-07 | Exxonmobil Res & Eng Co | Proceso de hidrotratamiento con manejo mejorado de hidrogeno. |
US9017547B2 (en) | 2005-07-20 | 2015-04-28 | Saudi Arabian Oil Company | Hydrogen purification for make-up gas in hydroprocessing processes |
-
2012
- 2012-11-02 WO PCT/US2012/063282 patent/WO2013067323A1/en active Application Filing
- 2012-11-02 CA CA2854364A patent/CA2854364C/en not_active Expired - Fee Related
- 2012-11-02 US US13/667,746 patent/US8968552B2/en active Active
- 2012-11-02 CN CN201280054187.2A patent/CN104011181B/zh not_active Expired - Fee Related
-
2015
- 2015-01-21 US US14/601,586 patent/US20150136649A1/en not_active Abandoned
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5114562A (en) * | 1990-08-03 | 1992-05-19 | Uop | Two-stage hydrodesulfurization and hydrogenation process for distillate hydrocarbons |
EP1063275A1 (fr) * | 1999-06-25 | 2000-12-27 | Institut Francais Du Petrole | Procédé d'hydrotraitement d'un distillat moyen dans deux zones comprenant une zone intermédiaire de stripage |
US7384540B2 (en) * | 2001-11-22 | 2008-06-10 | Institut Francais Du Petrole | Two-step method for middle distillate hydrotreatment comprising two hydrogen recycling loops |
CN100558446C (zh) * | 2005-01-21 | 2009-11-11 | 埃克森美孚研究工程公司 | 改进氢处理的馏出物两段加氢处理 |
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