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公开(公告)号：US4971681A
公开(公告)日：1990-11-20
申请号：US406475
申请日：1989-09-13
CPC分类号： B01J8/0055 , C10G11/18 , B01J2208/00132 , B01J2208/00548
摘要： A method and apparatus are disclosed to reduce the amount of unstripped hydrocarbon flowing to the regenerator in a riser reactor FCC unit. The catalyst stripper section is heated by indirect heat exchange with a mixture of hot regenerator flue gas and regenerated catalyst. In the preferred embodiment, the regenerator is operated under partial combustion conditions and the resulting carbon monoxide-containing flue gas is burned in a catalyst stripper heat exchanger.
摘要翻译： 公开了一种减少在提升管反应器FCC单元中流入再生器的未脱落碳氢化合物的量的方法和装置。 通过与热再生器烟道气和再生催化剂的混合物的间接热交换来加热催化剂汽提段。 在优选实施例中，再生器在部分燃烧条件下运行，并且所得一氧化碳的烟道气在催化剂汽提热交换器中燃烧。
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公开(公告)号：US5286691A
公开(公告)日：1994-02-15
申请号：US966475
申请日：1992-10-26
CPC分类号： C10G11/182 , B01J29/90 , B01J38/30 , Y10S502/516
摘要： A process for demetallizing metals contaminated FCC catalyst in an FCC regenerator. A metals getter additive, with higher settling velocity, is added to the regenerator, to remove metals from FCC catalyst by solid-solid interaction. The FCC catalyst forms a light, discrete, dense phase fluidized bed on top of a fluidized bed of additive. FCC catalyst is recycled to the cracking reactor from the top fluidized bed, while additive can be withdrawn from the lower fluidized bed for disposal or for metals recovery and recycle. Additive can be optimized for metals removal and will not dilute the cracking catalyst in the FCC reactor.
摘要翻译： 在FCC再生器中使金属污染的FCC催化剂脱金属的方法。 将一种具有较高沉降速度的金属吸附剂添加到再生器中，以通过固体 - 固体相互作用从FCC催化剂中除去金属。 FCC催化剂在添加剂流化床的顶部形成轻质，离散的致密相流化床。 FCC催化剂从顶部流化床再循环到裂化反应器中，而添加剂可从下流化床中排出以进行处理或用于金属回收和回收。 添加剂可以优化金属去除，不会稀释FCC反应器中的裂化催化剂。
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3.发明授权Process for producing gasoline having lower benzene content and distillation end point 失效具有较低苯含量和蒸馏终点的汽油生产方法
公开(公告)号：US5347061A
公开(公告)日：1994-09-13
申请号：US28057
申请日：1993-03-08
CPC分类号： C10G35/095 , C10G45/64 , C10G59/02
摘要： A process is disclosed for upgrading reformate and/or light FCC gasoline by substantially reducing the amount of benzene in the gasoline product while simultaneously reducing the gasoline ASTM distillation End Point. The process comprises the fractionation of reformate to recover that fraction, C.sub.7 -C.sub.8 hydrocarbons, directly useful in gasoline without further conversion. A heavy bottom fraction comprising C.sub.9 + aromatic and non-aromatic hydrocarbons is recovered and a C.sub.6 fraction rich in benzene. The total C.sub.6 fraction and a portion of the C.sub.9 + fraction are converted by alkylation, transalkylation and cracking in contact with acidic metallosilicate catalyst particles to gasoline boiling range materials rich in alkylaromatics. Following debutanization or depentanization of the conversion product, the fraction containing unconverted benzene is recycled to the reformate fractionator.
摘要翻译： 公开了一种用于通过显着减少汽油产物中苯的量来升级重整油和/或轻质FCC汽油的方法，同时同时还原汽油ASTM蒸馏终点。 该方法包括将重整产物分馏以回收该馏分，直接用于汽油而不进一步转化的C 7 -C 8烃。 回收包含C9 +芳烃和非芳烃的重底馏分和富含苯的C6馏分。 通过与酸性金属硅酸盐催化剂颗粒接触的烷基化，烷基转移和裂解转化为富含烷基芳族化合物的汽油沸点范围内的总C 6馏分和一部分C 9+馏分。 在转化产物的脱丁烷基化或去离子化之后，将含有未转化的苯的级分再循环至重整产物分馏塔。
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公开(公告)号：US5830346A
公开(公告)日：1998-11-03
申请号：US521177
申请日：1995-08-30
CPC分类号： C10G11/182 , B01D53/8625
摘要： Oxides of nitrogen (NO.sub.x) emissions from an FCC regenerator are reduced by operating the regenerator in partial CO burn mode to produce flue gas with more CO than O.sub.2 and with NO.sub.x precursors. This flue gas is then enriched with controlled amounts of oxygen and charged over catalyst, preferably Group VIII noble metal on a support, to convert most NO.sub.x precursors to nitrogen. Flue gas may then be charged to a CO boiler. Eliminating more than 90% of NO.sub.x emissions is possible by operating the FCC regenerator in partial CO burn mode, then adding air and catalytically converting NO.sub.x precursors at substoichiometric conditions. Conversion of NO.sub.x, if formed in the regenerator, may be achieved as well.
摘要翻译： 通过在部分CO燃烧模式下操作再生器来减少来自FCC再生器的氮（NOx）排放的氧化物，以产生具有比O 2和NO x前体更多的CO的烟道气。 然后，该烟道气用受控量的氧气富集，并通过催化剂，优选载体上的VIII族贵金属加入，以将大部分NOx前体转化为氮气。 然后将烟道气充入CO锅炉。 通过在部分CO燃烧模式下操作FCC再生器，然后在亚化学计量条件下添加空气和催化转化NOx前体，可以消除超过90％的NOx排放。 也可以在再生器中形成NOx的转化。
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公开(公告)号：US5382352A
公开(公告)日：1995-01-17
申请号：US963357
申请日：1992-10-20
CPC分类号： C10G11/182
摘要： Oxides of nitrogen (NO.sub.x) emissions from FCC regenerators in complete CO combustion mode are reduced by degrading regenerator performance to increase the coke on regenerated catalyst. High zeolite content cracking catalyst, regenerated to contain more coke, gives efficient conversion of feed and reduces NO.sub.x emissions from the regenerator. Operating with less catalyst, e.g., 30-60% of the normal amount of catalyst in the bubbling dense bed, can eliminate most NO.sub.x emissions while increasing slightly plant capacity and reducing catalyst deactivation.
摘要翻译： 通过降低再生器的性能，增加再生催化剂上的焦炭，可以降低FCC再生器在完全CO燃烧模式下的氮氧化物（NOx）排放。 再生含有更多焦炭的高沸石含量裂化催化剂能够有效地转化进料并减少再生器的NOx排放。 以较少的催化剂操作，例如起泡致密床中正常量的催化剂的30-60％可以消除大部分NOx排放物，同时增加轻微的装置容量并减少催化剂失活。
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公开(公告)号：US5389237A
公开(公告)日：1995-02-14
申请号：US28018
申请日：1993-03-08
IPC分类号： C10G11/18
CPC分类号： C10G11/18
摘要： A process for fluidized catalytic cracking of heavy feed using a low H.sub.2 S content lift gas in the base of a riser reactor. The lift gas is a recycled, ethylene rich stream obtained by removing H.sub.2 S from a compressed vapor stream intermediate the FCC main column receiver and the gas plant associated with the FCC unit. The low H.sub.2 S lift gas does not increase SO.sub.x emissions from the regenerator as much as a recycled vapor from the FCC main column. As the lift gas is not purified in the gas plant it does not overload it.
摘要翻译： 使用提升管反应器底部的低H 2 S含量提升气体的重质进料流化催化裂化的方法。 提升气体是通过从FCC主塔接收器和与FCC单元相关联的气体设备中的压缩蒸汽流除去H 2 S而获得的再循环的富乙烯流。 低H2S提升气体不会像来自FCC主塔的再循环蒸汽那样增加再生器的SO x排放。 由于提升气体在天然气厂不能净化，因此不会使其过载。
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公开(公告)号：US5599439A
公开(公告)日：1997-02-04
申请号：US322466
申请日：1994-10-14
CPC分类号： C10G69/08
摘要： A low sulfur gasoline of relatively high octane number is produced from a catalytically cracked, sulfur-containing naphtha by hydrodesulfurization followed by octane enhancing treatment in a fluidized bed catalytic process, in the presence of an aromatics-rich feedstream. The process converts the hydrodesulfurized intermediate and the aromatics-rich feedstream to a gasoline boiling range fraction of high octane number. The fluidized bed catalytic process is carried out over zeolite catalyst particles in a turbulent reactor bed at a temperature of about 600.degree. to 800.degree. F. (316.degree. to 427.degree. C.) and pressure of about 100 to 250 psig (790 to 825 kPa. The catalyst has an apparent particle density of about 0.9 to 1.6 g/cm.sup.3 and a size range of about 1 to 150 microns, and average catalyst particle size of about 20 to 100 microns containing about 10 to 25 weight percent of fine particles having a particle size less than 32 microns. The feed vapor is passed upwardly through the fluidized catalyst bed under turbulent flow conditions; turbulent fluidized bed conditions are maintained through the reactor bed between transition velocity and transport velocity at a superficial fluid velocity of about 0.3 to 2 meters per second. Treatment in the fluidized bed catalytic process restores the octane loss which takes place as a result of the hydrogenative treatment and results in a low sulfur gasoline product with an octane number comparable to that of the feed naphtha.
摘要翻译： 通过加氢脱硫，然后在富含芳烃的进料流存在下，在流化床催化方法中进行辛烷值增强处理，由催化裂解的含硫石脑油产生相对高辛烷值的低硫汽油。 该方法将加氢脱硫中间体和富含芳烃的进料流转化为高辛烷值的汽油沸程。 流化床催化过程在湍流反应器床中在沸点催化剂颗粒上进行，温度为约600至800°F（316至427℃），压力为约100至250psig（790至825 催化剂具有约0.9至1.6g / cm 3的表观颗粒密度和约1至150微米的尺寸范围，并且约20至100微米的平均催化剂颗粒尺寸含有约10至25重量％的具有 进料蒸气在湍流条件下向上通过流化催化剂床;湍流流化床条件通过反应器床保持在过渡速度和输送速度之间，表面流体速度约为0.3至2 流化床催化过程中的处理恢复了由于氢化处理而发生的辛烷值损失，导致低硫汽油产物与 辛烷值与进料石脑油相当。
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公开(公告)号：US5401387A
公开(公告)日：1995-03-28
申请号：US101810
申请日：1993-08-03
申请人： Mohsen N. Harandi , Hartley Owen
发明人： Mohsen N. Harandi , Hartley Owen
IPC分类号： C10G51/02
CPC分类号： C10G51/026
摘要： A process for multi-stage catalytic cracking is disclosed. A first stage cracks a first feed at atmospheric to 100 psig over a shape selective zeolite to convert from 10 to 90%, by volume, to lighter products rich in iso-compounds which may be used to make ethers. A second feed, which may include 700.degree. F.+ liquid from the selective cracking reaction, is cracked in a catalytic cracking (FCC) unit. Preferably all or some of the products from the shape selective cracking reactor are fractionated in the FCC main column.
摘要翻译： 公开了一种多级催化裂化方法。 第一阶段在形状选择性沸石上将大气压下的第一次进料裂解至100psig，将体积的10至90％转化成可用于制备醚的富含异构体的较轻质产物。 来自选择性裂解反应的可能包括700°F +液体的第二进料在催化裂化（FCC）单元中裂化。 优选地，来自形状选择性裂化反应器的所有或一些产物在FCC主塔中分馏。
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公开(公告)号：US5348707A
公开(公告)日：1994-09-20
申请号：US644141
申请日：1991-01-22
申请人： Mohsen N. Harandi , Hartley Owen
发明人： Mohsen N. Harandi , Hartley Owen
摘要： A multistage catalytic reactor system for preparing ethers such as methyl t-butyl (MTBE) and t-amyl methyl ether (TAME) from iso-olefin and methanol, comprising a first reactor for contacting the iso-olefin and alcohol with a solid regenerable catalyst, such as medium-pore zeolite conversion catalyst for partial conversion of the iso-olefin and methanol to an unsymmetrical ether, operatively connected for feeding effluent from the first reactor to a second etherification reaction zone containing sensitive catalyst, such as macroreticular polystyrenesulfonic acid resin. In a preferred embodiment, the second reaction zone comprises an inlet means for receiving withdrawn intermediate product, a catalytic distillation column containing solid acid resin etherification catalyst in a plurality of fixed bed catalysis-distillation zones, and outlet means for withdrawing a final etherification product.
摘要翻译： 一种用于从异烯烃和甲醇制备醚如甲基叔丁基（MTBE）和叔戊基甲基醚（TAME）的多级催化反应器系统，包括用于使异烯烃和醇与固体可再生催化剂接触的第一反应器 ，例如用于将异烯烃和甲醇部分转化成不对称醚的中孔沸石转化催化剂，其可操作地连接用于将来自第一反应器的流出物供给到包含敏感催化剂的大孔聚苯乙烯磺酸树脂的第二醚化反应区。 在优选的实施方案中，第二反应区包括用于接收取出的中间产物的入口装置，在多个固定床催化蒸馏区中含有固体酸树脂醚化催化剂的催化蒸馏塔和用于取出最终醚化产物的出口装置。
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10.发明授权Upgrading C4 mixed hydrocarbons by transhydrogenation and isobutene etherification 失效通过转氢和异丁烯醚化来升级C4混合烃
公开(公告)号：US5176719A
公开(公告)日：1993-01-05
申请号：US614479
申请日：1990-11-16
申请人： Mohsen N. Harandi , Hartley Owen
发明人： Mohsen N. Harandi , Hartley Owen
摘要： A technique for converting olefinic light hydrocarbons rich in butenes and butanes to ether-rich liquid fuels including etherification and transhydrogenation operations. The preferred process includes: reacting a mixed C4 hydrocarbon stream containing isobutene and n-butenes with lower aliphatic alcohol in an etherification zone in contact with an acidic etherification catalyst under etherification conditions whereby an effluent stream containing C5+ tertiary-alkyl ether is produced; separating the etherification effluent stream to provide a liquid stream comprising C5+ ether and an olefinic stream comprising unreacted C4 hydrocarbons; contacting at least the n-butenes from the C.sub.4 olefinic hydrocarbon stream with isobutane under transhydrogenation conditions in the presence of transhydrogenation catalyst whereby isobutane is converted to isobutene; separating transhydrogenation effluent to recover a C4 olefinic intermediate stream containing isobutene; and passing at least a portion of the isobutene-containing intermediate stream to the etherification zone for conversion to tertiary-alkyl ether.
摘要翻译： 将富含丁烯和丁烷的烯烃轻质烃转化为富含醚的液体燃料的技术，包括醚化和转氢操作。 优选的方法包括：在醚化条件下使含有异丁烯和正丁烯的混合C 4烃流与醚化区中的酸性醚化催化剂接触的低级脂族醇反应，从而产生含有C5 +叔烷基醚的流出物流; 分离醚化流出物流以提供包含C5 +醚和包含未反应的C 4烃的烯烃流的液体流; 在转氢催化剂的存在下，在转氢氢化条件下，使来自C4烯烃的至少一种烃与异丁烷接触，由此将异丁烷转化为异丁烯; 分离反氢化流出液以回收含有异丁烯的C 4烯烃中间体流; 并将至少一部分含异丁烯的中间物流送至醚化区转化为叔烷基醚。
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