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    • 1. 发明授权
    • Optimization of gas-to-liquids hydrocracker
    • 气 - 液加氢裂化器的优化
    • US07282139B2
    • 2007-10-16
    • US10886249
    • 2004-07-07
    • Rafael L. EspinozaKeith H. LawsonJianping Zhang
    • Rafael L. EspinozaKeith H. LawsonJianping Zhang
    • C10G47/00
    • C10G47/36Y10S208/95
    • A method for optimal production of synthetic diesel and naphtha from a hydrocracker includes hydrocracking a synthetic heavy hydrocarbon feed comprising an α value so as to form a diesel and a naphtha; selecting a desired diesel-to-naphtha ratio; calculating, based on the feed α and the desired diesel-to-naphtha ratio, a target molar ratio of hydrocarbons exiting to hydrocarbons entering the hydrocracker; and adjusting at least one hydrocracking conversion promoting condition so as to achieve said target molar ratio. The present invention further relates to a method for adjusting the overall production of a syngas-to-synthetic hydrocarbons plant in response to market conditions, comprising adjusting at least one hydrocracking conversion promoting condition and/or at least one conversion promoting condition within a Fischer-Tropsch reactor so as to maintain the overall diesel-to-naphtha ratio or to maintain a diesel production rate within a predetermined range of a desired value.
    • 从加氢裂化器最佳生产合成柴油和石脑油的方法包括加氢裂解包含α值的合成重质烃进料,以形成柴油和石脑油; 选择所需的柴油与石脑油比; 基于进料α和所需柴油与石脑油比计算出离开进入加氢裂化器的烃的烃的目标摩尔比; 并调节至少一种加氢裂化转化促进条件以达到所述目标摩尔比。 本发明还涉及一种用于响应于市场条件来调节合成气合成烃装置的总体生产的方法,其包括调节至少一种加氢裂化转化促进条件和/或至少一种转化促进条件在费 - 以保持整体柴油与石脑油的比例,或将柴油生产率保持在所需值的预定范围内。
    • 6. 发明授权
    • Commercial fischer-tropsch reactor
    • 商业费托反应堆
    • US07012103B2
    • 2006-03-14
    • US10395912
    • 2003-03-24
    • Rafael L. EspinozaJianping ZhangHarold A. WrightTodd H. Harkins
    • Rafael L. EspinozaJianping ZhangHarold A. WrightTodd H. Harkins
    • C07C27/00
    • C10G2/341B01J8/06B01J8/067B01J12/00B01J23/745B01J23/75B01J2208/00053B01J2208/00061B01J2208/00097B01J2208/00212
    • A process for producing hydrocarbons comprises providing a multi-tubular reactor having at least 100 tubes units containing a catalyst, each tube being between 2 and 5 meters tall and in thermal contact with a cooling fluid; feeding hydrogen and carbon monoxide to each tube at a linear gas superficial velocity less than about 60 cm/s; and converting the gas feedstream to hydrocarbons on the catalyst, wherein the yield of hydrocarbons in each tube is greater than 100 (kg hydrocarbons)/hr/(m3 reaction zone). Each tube may have an internal diameter greater than 2 centimeters. The catalyst may be active for Fischer Tropsch synthesis and may comprise cobalt or iron. The maximum difference in the radially-averaged temperature between two points that are axially spaced along the reactor is less than 15° C., preferably less than 10° C. The catalyst loading or intrinsic activity may vary along the length of the reactor.
    • 制备烃的方法包括提供具有至少100个含有催化剂的管单元的多管式反应器,每个管的高度在2和5米之间并与冷却流体热接触; 以低于约60cm / s的线性气体表观速度向每个管供给氢气和一氧化碳; 并将气体进料流转化为催化剂上的烃,其中每个管中的烃的产率大于100(kg碳氢化合物)/ hr /(m 3)反应区)。 每根管子的内径可以大于2厘米。 该催化剂可用于费 - 托合成,并且可以包含钴或铁。 沿着反应器轴向间隔的两个点之间的径向平均温度的最大差异小于15℃,优选小于10℃。催化剂负载或固有活性可以沿着反应器的长度而变化。