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    Heavy oil hydrogasification process
    5.
    发明授权
    Heavy oil hydrogasification process 失效
    重油加氢气化工艺

    公开(公告)号：US3891404A

    公开(公告)日：1975-06-24

    申请号：US33954573

    申请日：1973-03-09

    申请人： INST GAS TECHNOLOGY

    发明人： WEIL SANFORD A ,  TARMAN PAUL B ,  PUNWANI DHARAMVIR

    IPC分类号： C10G47/28 ,  C10G13/16

    CPC分类号： C10G47/28 ,  C10G2400/26

    摘要： A process for producing a high methane content, synthetic pipeline gas from heavy fuel oils including crude oil, Bunker ''''C'''' residual oil, shale oil, and solubilized coal. The process includes providing a hydrogasification reaction chamber having a hydrogen partial pressure of at least 100 psig and a temperature of 1200*-1500*F. Absorbent inert solids are recirculated from the bottom of the reaction chamber to the top thereof and the heavy fuel oil is introduced into the recirculating solids and both are fed to the top of the reaction chamber. The reaction chamber includes an oil preheat zone having a temperature up to 1000*F., a reaction zone at a temperature of 1200*-1500*F. and a hydrogen preheat zone, also having a temperature of 1200*-1500*F. The solids are moved through the chamber so that the oil is gradually heated to the reaction temperature over a period of at least ten minutes to inhibit the formation of a coke residue. A hydrogen rich gas, containing hydrogen in excess of stoichiometric amounts, is passed upwardly in the reaction chamber and countercurrent to the heavy oil and solids passing downwardly therethrough. A hydrogenation reaction is promoted in the reaction chamber between the oil and hydrogen to produce a mixture which includes volatilized liquids, methane and hydrogen. The mixture is separated into a hydrogasifiable liquid fraction, hydrogen, and the high methane content synthetic pipeline gas. The hydrogen and the hydrogasifiable liquid fraction are circulated back to the reaction chamber, the hydrogen being used as at least a portion of the hydrogen rich gas reacting in the chamber and the hydrogasifiable liquid enters into the hydrogenation reaction.

    摘要翻译： 用于生产高甲烷含量的方法，包括原油，Bunker“C”残油，页岩油和溶解煤等重质燃料油的合成管道气。 该方法包括提供具有至少100psig的氢分压和1200-1500°F的温度的加氢气化反应室。吸收性惰性固体从反应室的底部再循环到其顶部，重质燃料油 被引入再循环固体中，并且两者都被供给到反应室的顶部。 反应室包括温度高达1000°F的油预热区域，温度为1200°-15°F的反应区域和温度为1200°-1500°F的氢气预热区域。 将固体移动通过室，使得油在至少十分钟的时间内逐渐加热至反应温度以抑制焦炭残留物的形成。 含有超过化学计量量的氢的富氢气体在反应室中向上通过，并与通过其中的向下通过的重油和固体逆流。 在油和氢之间的反应室中促进氢化反应以产生包含挥发液体，甲烷和氢气的混合物。 将混合物分离成可加氢气化的液体馏分，氢气和高甲烷含量的合成管道气体。 氢气和可加氢气体的液体馏分循环回反应室，氢气用作在室中反应的富氢气体的至少一部分，并且可加氢气体的液体进入氢化反应。

    Moving Bed Hydrocarbon Conversion Process
    6.
    发明申请
    Moving Bed Hydrocarbon Conversion Process 审中-公开
    移动床烃转化过程

    公开(公告)号：US20100187159A1

    公开(公告)日：2010-07-29

    申请号：US12361181

    申请日：2009-01-28

    申请人： Christopher Naunheimer

    发明人： Christopher Naunheimer

    IPC分类号： C10G35/14

    CPC分类号： C10G35/12 ,  B01J8/125 ,  C10G47/28 ,  C10G49/14

    摘要： Moving bed hydrocarbon conversion processes are provided for contacting a catalyst moving downward through a reaction zone with a hydrocarbon feed, withdrawing the catalyst from the reaction zone and conveying the catalyst to a regeneration zone wherein the catalyst moves downward. The catalyst is withdrawn from the regeneration zone and passed downward to an upper zone of a particle transfer apparatus wherein the transfer of catalyst from the upper zone through a middle zone to a lower zone is regulated by varying the pressure of the middle zone, the flow rate of gas passing through an upper valveless conduit, and a valve in a lower valved conduit. The catalyst from the lower zone of the particle transfer apparatus is conveyed to the reactions zone.

    摘要翻译： 提供了移动床烃转化方法，用于使向下移动通过反应区的催化剂与烃进料接触，将催化剂从反应区取出并将催化剂输送到催化剂向下移动的再生区。 催化剂从再生区抽出并向下传送到颗粒转移装置的上部区域，其中催化剂从上部区域通过中间区域转移到下部区域是通过改变中间区域的压力来调节的 通过上部无阀管道的气体速率和下部阀门管道中的阀门。 来自颗粒转移装置的下部区域的催化剂被输送到反应区。

    H-oil process
    7.
    发明授权
    H-oil process 失效
    H油过程

    公开(公告)号：US3888761A

    公开(公告)日：1975-06-10

    申请号：US37179273

    申请日：1973-06-20

    申请人： CITIES SERVICE RES & DEV CO

    发明人： STEWART NORMAN C

    IPC分类号： C10G45/20 ,  C10G47/28 ,  C10G1/08 ,  C10G13/00

    CPC分类号： C10G45/20 ,  C10G47/28

    摘要： A process and apparatus are shown for the improved utilization of catalysts in a hydrocracking system. The method comprises passing a hydrocarbon oil feedstock, preferably a heavy hydrocarbon residuum, upwardly through a particulate catalyst bed in a reaction zone maintained at high temperature and high pressure, together with hydrogen-containing gas; recycling a portion of the upwardly flowing oil together with a portion of the particulate catalyst to the bottom of the reaction zone while simultaneously pulverizing the minor proportion of the particulate catalyst to a fine powdered catalyst; and passing the recycled oil and finely powdered catalyst upwardly through the particulate catalyst bed in the reaction zone, with at least a portion of the powdered catalyst leaving the reactor with the treated effluent. Apparatus for practicing this process comprises a reactor vessel having a vertically mounted recycle conduit mounted therein, and pulverizing means, preferably a modified axial turbine high-shear mixer communicatingly connected to the bottom of the recycle conduit, for pulverizing recycled particulate catalyst to a fine powdery catalyst. Additionally, a pump is mounted to the outlet of the high-shear turbine mixer to provide positive fluid flow.

    Startup method for exothermic catalytic reaction zones
    8.
    发明授权
    Startup method for exothermic catalytic reaction zones 失效
    放热催化反应区的启动方法

    公开(公告)号：US3873440A

    公开(公告)日：1975-03-25

    申请号：US41852573

    申请日：1973-11-14

    申请人： UNIVERSAL OIL PROD CO

    发明人： HALLMAN NEWT M

    IPC分类号： C10G49/24 ,  C10G13/16

    CPC分类号： C10G49/24 ,  C10G47/28 ,  C10G2300/4031

    摘要： Direct fired charge heaters are deleted from the equipment needed to start an exothermic catalytic hydrocarbon conversion process by changing the flow through the high pressure heat exchangers normally used to recover heat from the reactor effluent. Instead, heat produced in a product fractionation heater is added to a reactor effluent recirculation loop containing the reactor by the use of these heat exchangers. The heat exchanged reactor effluent is returned to the reactor with a recycle pump until the temperature of this charge stream is sufficient to initiate the exothermic reaction and thereby produce a hot effluent stream which is used to heat fresh charge material.

    摘要翻译： 通过改变通过通常用于从反应器流出物回收热量的高压热交换器的流量，从开始放热催化烃转化过程所需的设备中删除直接燃烧的充电加热器。 相反，在产品分馏加热器中产生的热量通过使用这些热交换器被添加到包含反应器的反应器流出物循环回路中。 将热交换的反应器流出物用回收泵返回到反应器中，直到该进料流的温度足以引发放热反应，从而产生用于加热新鲜进料的热流出物流。