利索-全球专利检索

  1. 登录
  2. 注册

搜索结果

168 条记录 (耗时 0.025 秒)

    APPARATUSES AND METHODS FOR CRACKING HYDROCARBONS
    6.
    发明申请
    APPARATUSES AND METHODS FOR CRACKING HYDROCARBONS 有权
    破碎油料的装置和方法

    公开(公告)号：US20150322355A1

    公开(公告)日：2015-11-12

    申请号：US14274540

    申请日：2014-05-09

    申请人： UOP LLC

    发明人： Trung Pham ,  Lev Davydov ,  Lance Awender Baird

    IPC分类号： C10G51/06 ,  B01J8/26 ,  C10G55/00

    CPC分类号： B01J8/26 ,  B01J2208/00991 ,  C10G3/42 ,  C10G51/06 ,  C10G55/00 ,  C10G69/00 ,  C10G2300/1014 ,  C10G2300/1077 ,  C10G2300/4056 ,  Y02P30/20

    摘要： Methods and apparatuses are provided for cracking a hydrocarbon. The method includes contacting a first hydrocarbon stream with a first cracking catalyst at a first cracking temperature in a first riser to produce a first riser effluent and a first spent catalyst. A second hydrocarbon stream is contacted with a second cracking catalyst at a second cracking temperature in a second riser to produce a second riser effluent and a second spent catalyst, where the second cracking temperature is less than the first cracking temperature. The first riser effluent and the second riser effluent are combined to produce a mixed riser effluent, and the mixed riser effluent is fractionated in a fractionation zone to produce a light cycle oil. The first spent catalyst and the second spent catalyst are combined in a reactor to produce a mixed spent catalyst.

    摘要翻译： 提供了开裂烃的方法和装置。 该方法包括使第一烃流与第一裂解催化剂在第一提升管中以第一裂解温度接触以产生第一提升管流出物和第一废催化剂。 第二烃流在第二提升管中以第二裂解温度与第二裂解催化剂接触以产生第二提升管流出物和第二废催化剂，其中第二裂解温度小于第一裂解温度。 将第一提升管流出物和第二提升管流出物混合以产生混合提升管流出物，并将混合提升管流出物在分馏区中分馏以产生轻循环油。 将第一废催化剂和第二废催化剂在反应器中混合以产生混合的废催化剂。

    Process for cracking heavy hydrocarbon feed
    7.
    发明授权
    Process for cracking heavy hydrocarbon feed 有权
    裂解重烃进料的方法

    公开(公告)号：US08658023B2

    公开(公告)日：2014-02-25

    申请号：US12980514

    申请日：2010-12-29

    申请人： Steven T. Coleman

    发明人： Steven T. Coleman

    IPC分类号： C10G69/04 ,  C10G69/06 ,  C10G55/06 ,  C10G51/02 ,  C10G9/36

    CPC分类号： C10G11/20 ,  C10G51/06 ,  C10G69/00 ,  C10G2300/301 ,  C10G2300/807 ,  C10G2400/02 ,  C10G2400/20

    摘要： A hydrocarbon feed is passed to a first zone of a vaporization unit to separate a first vapor stream and a first liquid stream. The first liquid stream is passed to a second zone of the vaporization unit and contacted with a counter-current steam to produce a second vapor stream and a second liquid stream. The first vapor stream and the second vapor stream are cracked in the radiant section of the steam cracker to produce a cracked effluent. The second liquid stream is catalytically cracked to produce a cracked product. The cracked product is distilled to produce an overhead stream, a light cycle oil, and a heavy cycle oil. The light cycle oil is reacted with hydrogen in the presence of a catalyst to produce a hydrotreated light cycle oil. The hydrotreated light cycle oil and the overhead stream are fed to the vaporization unit.

    摘要翻译： 烃进料通过蒸发单元的第一区域以分离第一蒸气流和第一液体流。 第一液体流被传送到蒸发单元的第二区域并与逆流蒸汽接触以产生第二蒸气流和第二液体流。 第一蒸汽流和第二蒸汽流在蒸汽裂解器的辐射部分中裂开以产生裂化流出物。 第二液体流被催化裂化以产生裂化产物。 将裂化产物蒸馏以产生塔顶馏出物流，轻循环油和重循环油。 轻链循环油在催化剂存在下与氢气反应以产生加氢处理的轻循环油。 将加氢处理的轻循环油和塔顶馏分油进料至汽化装置。

    FCC PROCESS FOR MAXIMIZING DIESEL
    8.
    发明申请
    FCC PROCESS FOR MAXIMIZING DIESEL 审中-公开
    用于最大化柴油的FCC方法

    公开(公告)号：US20140034551A1

    公开(公告)日：2014-02-06

    申请号：US14111145

    申请日：2011-04-15

    申请人： Emanuel Freire Sandes ,  Leandro Morais Silva ,  William Richard Gilbert ,  Jose Geraldo Furtado Ramos

    发明人： Emanuel Freire Sandes ,  Leandro Morais Silva ,  William Richard Gilbert ,  Jose Geraldo Furtado Ramos

    IPC分类号： C10G11/18

    CPC分类号： C10G11/18 ,  C10G51/06 ,  C10G2300/1048 ,  C10G2300/4056 ,  C10G2400/02 ,  C10G2400/04

    摘要： A process is described for maximizing the FCC middle distillates comprising the use of two different converters, operating in a coordinated manner that seeks to maximize the production of LCO for diesel, generating a specified gasoline and reducing fuel oil production. Converter “A” operates with a low contact time in the riser, of 0.2 to 1.5 sec. (preferably from 0.5 to 1.0 sec.) making a higher reaction temperature possible even at low severity, from 510° C. to 560° C. (preferably from 530° C. to 550° C.) and with a catalyst suitable to the maximization of LCO. Converter “B” possesses a high activity catalytic system, suited to cracking naphtha and DO generated in the first converter. Preferably, converter “B” has two separate risers, allowing the reaction temperatures of each to be adjusted independently according to the range most recommended for maximizing the cracking of each of the streams: 530° C. to 560° C. for the DO riser and 540° C. to 600° C. for the naphtha riser. The high-quality LCO stream generated by cracking at low severity in converter “A” is not contaminated by the poorer quality LCO generated by re-cracking the DO in converter “B,” since each converter has its own fractionating tower. The use of low contact time as a route for reducing severity in converter “A” geared towards the production of better quality LCO allows it to operate with a higher reaction temperature for the same LCO conversion and quality level, entailing greater operating reliability for the unit, and providing benefits for the heat balance of the converter. In existing units, the improvement in the heat balance provides leeway to the air blower via increased batch temperature, and makes room for processing more residual batches.

    摘要翻译： 描述了一种最大化FCC中间馏分的方法，其包括使用两种不同的转化器，以协调的方式运行，其寻求最大化柴油的LCO生产，产生特定的汽油和减少燃料油的生产。 转换器“A”在提升管中的接触时间低，为0.2至1.5秒。 （优选为0.5至1.0秒），甚至在较低的苛刻度下也可以使用更高的反应温度，从510℃至560℃（优选530℃至550℃）和适合于 LCO最大化。 转化器“B”具有高活性催化系统，适用于在第一转化器中产生的石脑油和DO。 优选地，转化器“B”具有两个单独的提升管，允许每个反应温度根据最适合使每个流的最大化的范围独立地调节：对于DO提升管为530℃至560℃ 对于石脑油提升管为540℃至600℃。 由于每个转换器都有自己的分馏塔，所以在转换器“A”中以低严重程度开裂产生的高质量LCO流不会被转换器“B”中的DO重新开裂所产生的较差的质量LCO所污染。 使用低接触时间作为降低转换器“A”的严重性的路线，用于生产更好质量的LCO，使其能够在相同的LCO转换和质量水平下以更高的反应温度运行，从而为该单元提供更高的运行可靠性 ，并为转换器的热平衡提供益处。 在现有单元中，热平衡的改善通过增加批量温度为鼓风机提供了余地，并且为处理更多的剩余批次提供了空间。

    Process for Cracking Heavy Hydrocarbon Feed
    10.
    发明申请
    Process for Cracking Heavy Hydrocarbon Feed 有权
    破碎重烃进料的工艺

    公开(公告)号：US20120125811A1

    公开(公告)日：2012-05-24

    申请号：US12952662

    申请日：2010-11-23

    申请人： Robert S. Bridges ,  Sellamuthu G. Chellappan

    发明人： Robert S. Bridges ,  Sellamuthu G. Chellappan

    IPC分类号： C10G69/06

    CPC分类号： C10G45/00 ,  C10G9/005 ,  C10G9/20 ,  C10G9/36 ,  C10G47/00 ,  C10G51/06 ,  C10G69/00 ,  C10G69/06 ,  C10G2300/301 ,  C10G2300/807 ,  C10G2400/20

    摘要： A process for cracking a heavy hydrocarbon feed comprising a vaporization step, a coking step, a hydroprocessing step, and a steam cracking step is disclosed. The heavy hydrocarbon feed is passed to a first zone of a vaporization unit to separate a first vapor stream and a first liquid stream. The first liquid stream is passed to a second zone of the vaporization unit and contacted intimately with a counter-current steam produce a second vapor stream and a second liquid stream. The first vapor stream and the second vapor stream are cracked in the radiant section of the steam cracker to produce a cracked effluent. The second liquid stream is thermally cracked in a coking drum to produce a coker effluent and coke. The coker effluent is separated into a coker gas and a coker liquid. The coker liquid is reacted with hydrogen in the presence of a catalyst to produce a hydroprocessed product. The hydroprocessed product is separated into a gas product and a liquid product. The liquid product is fed to the vaporization unit.

    摘要翻译： 公开了一种用于裂化重质烃进料的方法，包括蒸发步骤，焦化步骤，加氢处理步骤和蒸汽裂解步骤。 将重质烃进料通入蒸发单元的第一区域以分离第一蒸气流和第一液体流。 第一液体流被传送到蒸发单元的第二区域并与逆流蒸汽紧密接触产生第二蒸气流和第二液体流。 第一蒸汽流和第二蒸汽流在蒸汽裂解器的辐射部分中裂开以产生裂化流出物。 第二液体流在焦化鼓中热裂化以产生焦化器流出物和焦炭。 焦化流出物被分离成焦化气体和焦化液。 在催化剂存在下，将焦化液与氢气反应，生成加氢产物。 加氢处理的产物被分离成气体产物和液体产物。 将液体产物送入汽化装置。