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    FLUID CATALYTIC CRACKING (FCC) PROCESS FOR MANUFACTURING PROPYLENE AND ETHYLENE IN INCREASED YIELD
    1.
    发明申请
    FLUID CATALYTIC CRACKING (FCC) PROCESS FOR MANUFACTURING PROPYLENE AND ETHYLENE IN INCREASED YIELD 有权
    流化床催化裂化（FCC）在增加乙烯和乙烯中制备丙烯和乙烯的方法

    公开(公告)号：US20110240523A1

    公开(公告)日：2011-10-06

    申请号：US13133759

    申请日：2009-12-08

    Applicant: Sukumar Mandal ,  Asit Kumar Das ,  Ashwani Yadav ,  Manoj Yadav ,  Akhilesh Bhatnagar ,  Rajeshwar Dongara ,  Veera Venkata satya Bhaskara sita Rama Murthy Katravulapalli

    Inventor： Sukumar Mandal ,  Asit Kumar Das ,  Ashwani Yadav ,  Manoj Yadav ,  Akhilesh Bhatnagar ,  Rajeshwar Dongara ,  Veera Venkata satya Bhaskara sita Rama Murthy Katravulapalli

    IPC: C10G11/04

    CPC classification number: C10G11/18 ,  C10G11/05 ,  C10G2400/20

    Abstract: A fluid catalytic cracking (FCC) process for manufacturing propylene and ethylene in increased yield. The process comprises cracking an olefinic naphtha stream and main hydrocarbon stock in combination with an olefinic C4 hydrocarbon stream in different zones of one or more risers of an FCC unit. Each FCC riser comprises an acceleration zone at the lower portion thereof, a lift stream feed nozzle at the bottom of the acceleration zone, a main hydrocarbon stock feed nozzle above the acceleration zone and an olefinic naphtha feed nozzle at a location along the acceleration zone between the lift stream feed nozzle and main hydrocarbon stock feed nozzle. The cracking is carried out on a mixed FCC catalyst comprising at least 2 percent by weight pentasil zeolite and at least 10 percent by weight Y-zeolite. The catalyst is injected at the bottom of each FCC riser, the olefinic naptha is injected through the olefinic feed nozzle, the main hydrocarbon stock is injected through the main hydrocarbon stock feed nozzle and the lift stream is injected through the lift stream feed nozzle at the bottom of the acceleration zone. The lift stream comprises the olefinic C4 hydrocarbon stream with or without steam and/or a fuel gas. The olefinic C4 hydrocarbon steam is cracked in the acceleration zone at 600 to 8000° C. and pressure of 0.8 to 5 kg/cm up 2 (gauge) and weight hourly space velocity (WHSV) of 0.2 to 100 hr up 1 and vapour residence time of 0.2 to 5 seconds.

    Abstract translation: 用于以增加的产率制造丙烯和乙烯的流化催化裂化（FCC）方法。 该方法包括在FCC单元的一个或多个立管的不同区域中与烯属烃石脑油流和主要烃类物料一起裂化。 每个FCC提升管包括其下部的加速区，加速区底部的升力流进料喷嘴，加速区上方的主烃储料供给喷嘴和沿加速区的位置处的烯烃石脑油进料喷嘴， 升降机进料喷嘴和主油料进料喷嘴。 裂化在包含至少2重量百分比的pentasil沸石和至少10重量％Y-沸石的混合FCC催化剂上进行。 在每个FCC提升管的底部注入催化剂，通过烯烃进料喷嘴注入烯烃萘，主要烃类原料通过主要烃类原料进料喷嘴注入，提升流通过提升料流进料喷嘴注入 底部的加速区。 提升流包括具有或不具有蒸汽和/或燃料气体的烯烃C4烃流。 烯烃C4烃蒸汽在600-8000℃的加速区裂化，压力为0.8-5kg / cm 2（表压），重时空速（WHSV）为0.2〜100小时-1，蒸汽停留 时间为0.2〜5秒。

    Fluidized catalytic cracking process
    3.
    发明授权
    Fluidized catalytic cracking process 有权
    流化催化裂化工艺

    公开(公告)号：US06267873B1

    公开(公告)日：2001-07-31

    申请号：US09201896

    申请日：1998-11-30

    Applicant: Asit Kumar Das ,  Debasis Bhattacharyya ,  Sukumar Mandal ,  Vutukuru Lakshmi Narasimha Murthy ,  Sanjeev Singh ,  Marri Rama Rao ,  Sobhan Ghosh

    Inventor： Asit Kumar Das ,  Debasis Bhattacharyya ,  Sukumar Mandal ,  Vutukuru Lakshmi Narasimha Murthy ,  Sanjeev Singh ,  Marri Rama Rao ,  Sobhan Ghosh

    IPC: C10G1100

    CPC classification number: C10G11/187 ,  C10G11/18 ,  Y10S585/91

    Abstract: A fluidized catalytic cracking process for catalytically cracking a feed to lighter products includes introducing a heated catalyst and the feed into a bottom riser of a fluidized catalytic cracking apparatus and allowing the heated catalyst and the feed to preaccelerate upwardly within the bottom riser as a mixture; flowing the mixture upwardly from the bottom riser through a plurality of microriser tubes disposed within a regenerator under conditions effective to cause a cracking reaction of the hydrocarbons and result in a mixture including coked catalyst and hydrocarbon vapors; passing the mixture from the microriser tubes through a catalyst separator for separating the coked catalyst from the hydrocarbon vapors; collecting coked catalyst in a stripper for stripping out hydrocarbon vapors carried along with the coked catalyst and introducing the coked catalyst collected into a regenerator; simultaneous with flowing the mixture, combusting the coked catalyst within the regenerator under conditions effective to cause regeneration of the catalyst so that hot regenerated catalyst is produced and heat transferred to the microriser tubes; introducing the hot regenerated catalyst from the regenerator into the bottom riser for facilitating continuous operation; and directing hydrocarbon vapors from the catalyst separator and from the stripper to a fractionator for separation of products.

    Abstract translation: 将进料催化裂化成较轻产物的流化催化裂化方法包括将加热的催化剂和进料引入流化催化裂化装置的底部提升管中，并允许加热的催化剂和进料作为混合物在底部提升管内向前预加速; 在有效引起烃的裂解反应并产生包括焦化催化剂和烃蒸汽的混合物的条件下，将混合物从底部提升管向上流过设置在再生器内的多个微型管; 将混合物从微循环管通过催化剂分离器，用于将焦化的催化剂与烃蒸气分离; 在汽提器中收集焦化的催化剂，用于汽提与焦炭催化剂一起携带的烃蒸气并将收集的焦化催化剂引入再生器中; 同时使混合物流动，在有效使催化剂再生的条件下在再生器内燃烧焦化催化剂，使得产生热再生催化剂并将热量传递至微型管; 将热再生催化剂从再生器引入底部提升管，以便于连续操作; 并将碳氢化合物蒸汽从催化剂分离器和汽提器引导至用于分离产物的分馏器。

    Process for catalytic cracking of petroleum based feed stocks
    4.
    发明授权
    Process for catalytic cracking of petroleum based feed stocks 失效
    石油基原料催化裂化工艺

    公开(公告)号：US5846402A

    公开(公告)日：1998-12-08

    申请号：US855946

    申请日：1997-05-14

    Applicant: Sukumar Mandal ,  Suresh Kumarshah ,  Debasis Bhattacharyya ,  Vutukuru Lakshmi Narasimha Murthy ,  Asit Kumar Das ,  Sanjeev Singh ,  Ram Mohan Thakur ,  Shankar Sharma ,  Jagdev Kumar Dixit ,  Sobhan Ghosh ,  Satyen Kumar Das ,  Manoranjan Santra ,  Latoor Lal Saroya ,  Marri Rama Rao ,  Ganga Shanker Mishra ,  Satish Makhija

    Inventor： Sukumar Mandal ,  Suresh Kumarshah ,  Debasis Bhattacharyya ,  Vutukuru Lakshmi Narasimha Murthy ,  Asit Kumar Das ,  Sanjeev Singh ,  Ram Mohan Thakur ,  Shankar Sharma ,  Jagdev Kumar Dixit ,  Sobhan Ghosh ,  Satyen Kumar Das ,  Manoranjan Santra ,  Latoor Lal Saroya ,  Marri Rama Rao ,  Ganga Shanker Mishra ,  Satish Makhija

    IPC: B01J29/80 ,  C10G11/05 ,  C10G11/18 ,  C10G11/00

    CPC classification number: B01J29/80 ,  C10G2400/20 ,  C10G2400/28

    Abstract: A process for selective catalytic cracking of a petroleum-based feedstock to produce a product having a high yield of liquified petroleum gas (LPG) and light olefins having 3 to 4 carbons includes providing a fluidized bed reactor which is a high velocity riser, continuously circulating fluidized bed reactor; providing a solid acidic catalyst comprised of: from 1 to 6% by wt. of ultra stable Y-zeolite; from 8-25% by wt. of Pentasil zeolite which is shape selective; from 0-8% by wt. of an active material which is bottom selective; from 0-1% by wt. of rare earth constituents; and from 91 to 60% by wt. of nonacidic constituents and binder; charging the fluidized bed reactor with the solid acidic catalyst and the petroleum-based feedstock; and cracking the petroleum-based feedstock in the presence of the solid acidic catalyst in the fluidized bed reactor. The reactor is operated at a Weight Hourly Space Velocity (WHSV) ranging from 40 to 120 hr.sup.-1, a ratio of solid acidic catalyst to petroleum-based feedstock ranging from 15 to 25, a temperature at the top of the high velocity riser ranging from 530.degree. C. to 600.degree. C., recycled riser products ranging from 0 to 40%, a pressure in the fluidized bed reactor ranging from 1.0 to 4.0 kg/cm.sup.2 g, and an amount of steam for dilution and quenching of hydrocarbons ranging from 3 to 50 wt. % of the petroleum-based feedstock. The Pentasil zeolite has a pore size ranging from 5 to 6 .ANG. so that the catalyst is highly selective for LPG and C.sub.4 light olefins with minimum dry gas and coke make, and so that the vanadium tolerance of the catalyst is increased and ranges up to 21,000 PPM. The process produces a LPG yield ranging up to 40 to 65 wt. % of the fresh petroleum-based feedstock, a selectivity for the light olefins of at least 40 wt. %, and a selectivity for the LPG of at least 45 wt.

    Abstract translation: 选择性催化裂化石油基原料以生产具有高产率的液化石油气（LPG）和具有3至4个碳原子的轻质烯烃的产物的方法包括提供流化床反应器，其为高速提升管，连续循环 流化床反应器; 提供固体酸性催化剂，其包含：1至6重量％ 的超稳定Y型沸石; 8-25重量％。 具有形状选择性的pentasil沸石; 0-8重量％ 的底部选择性活性物质; 0-1重量％ 的稀土成分; 和91〜60重量％。 的非酸成分和粘合剂; 用固体酸性催化剂和石油基原料装入流化床反应器; 并在流化床反应器中在固体酸性催化剂存在下裂化石油基原料。 反应器以40至120小时-1的重量小时空间速度（WHSV）运行，固体酸性催化剂与石油基原料的比例为15至25，高速提升管顶部的温度范围 从530℃至600℃，循环的提升产品的范围为0至40％，流化床反应器的压力范围为1.0至4.0kg / cm2g，以及用于稀释和猝灭烃的蒸汽量 3〜50重量％ ％的石油基原料。 Pentasil沸石的孔径范围为5至6安格姆，使得催化剂对于具有最少干燥气体和焦炭的LPG和C4轻质烯烃具有高选择性，并且使得催化剂的耐钒性增加并且范围高达21,000 PPM。 该方法产生高达40至65重量％的LPG产率。 ％的新鲜石油基原料，轻质烯烃的选择性至少为40wt。 ％，并且LPG的选择性至少为45wt。

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