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    Method of hydroisomerizing paraffins emanating from the Fischer-Tropsch process using catalysts based on H-Y zeolite
    1.
    发明授权
    Method of hydroisomerizing paraffins emanating from the Fischer-Tropsch process using catalysts based on H-Y zeolite 失效
    使用基于H-Y沸石的催化剂从费 - 托方法发出的烷烃加氢异构化方法

    公开(公告)号：US5306860A

    公开(公告)日：1994-04-26

    申请号：US886224

    申请日：1992-05-21

    申请人： Pierre-Henri Bigeard ,  Alain Billon ,  Pierre Dufresne ,  Samuel Mignard

    发明人： Pierre-Henri Bigeard ,  Alain Billon ,  Pierre Dufresne ,  Samuel Mignard

    IPC分类号： C10G65/04 ,  C07C5/13 ,  C07C5/22

    CPC分类号： C10G65/043 ,  Y10S208/95 ,  Y10S585/946

    摘要： For Hydroisomerizering charges emanating from the Fischer-Tropsch process:a) hydrogen is reacted with the charge in contact with a catalyst 1 in a first reaction zone, the catalyst 1 comprising at least one alumina-based matrix and at least one hydro-dehydrogenation component andb) the effluent from the first reaction zone is put into contact with a catalyst 2 in a second reaction zone, the catalyst 2 comprising:20 to 97% by weight of at least one matrix,3 to 80% by weight of at least one Y zeolite in hydrogen form, the zeolite being characterized by an SiO.sub.2 /Al.sub.2 O.sub.3 molar ratio of over 4.5; a sodium content of less than 1% by weight determined at 1100.degree. C. under calcining conditions; an a.sub.o crystal parameter of the elemental mesh of less than 24.70.times.10.sup.-10 m; and a specific surface area determined by the BET method of over 400 m.sup.2.g.sup.-1, andat least one hydro-dehydrogenation component.

    摘要翻译： 对于从费 - 托方法产生的加氢异构化电荷：a）氢与在第一反应区中与催化剂1接触的电荷反应，催化剂1包含至少一种基于氧化铝的基体和至少一个氢脱氢组分 和b）来自第一反应区的流出物与第二反应区中的催化剂2接触，催化剂2包含：至少一种基质20至97重量％，至少3至80重量％ 一种Y型沸石为氢形式，沸石的特征在于SiO 2 / Al 2 O 3摩尔比超过4.5; 在1100℃下在煅烧条件下测定的钠含量小于1重量％ 元素网的ao晶体参数小于24.70×10-10 m; 并且通过BET法测定的比表面积超过400m 2·g -1，和至少一种加氢脱氢组分。

    Method of hydrocracking paraffins emanating from the Fischer-Tropsch process using catalysts based on H-Y zeolite
    2.
    发明授权
    Method of hydrocracking paraffins emanating from the Fischer-Tropsch process using catalysts based on H-Y zeolite 失效
    使用基于H-Y沸石的催化剂从费 - 托方法发出的链烷烃的加氢裂化方法

    公开(公告)号：US5345019A

    公开(公告)日：1994-09-06

    申请号：US886225

    申请日：1992-05-21

    申请人： Pierre-Henri Bigeard ,  Alain Billon ,  Pierre Dufresne ,  Samuel Mignard

    发明人： Pierre-Henri Bigeard ,  Alain Billon ,  Pierre Dufresne ,  Samuel Mignard

    IPC分类号： C10G65/10 ,  C07C5/00 ,  C07C5/42

    CPC分类号： C10G65/10 ,  Y10S585/946

    摘要： A method of hydrocracking charges emanating from the Fischer-Tropsch process, in which:(a) hydrogen is reacted with the charge in contact with a catalyst 1 in a first reaction zone, the said catalyst 1 comprising at least one alumina-based matrix and at least one hydro-dehydrogenation component;(b) the effluent from the first reaction zone is put into contact with a catalyst 2 in a second reaction zone, the said catalyst 2 comprising:20 to 97% by weight of at least one matrix;3 to 80% by weight of at least one Y zeolite in hydrogen form,the said zeolite being characterized by an SiO.sub.2 /Al.sub.2 O.sub.3 molar ratio of over 4.5:1, a sodium content of less than 1% by weight determined on a zeolite calcined at 1100.degree. C.; an a.sub.o crystal parameter of the elemental mesh of less than 24.70.times.10.sup.-10 m; and a specific surface area determined by the BET method of over 400 m.sup.2.g.sup.-1 ;and at least one hydro-dehydrogenation component.

    摘要翻译： 一种从费 - 托法生产的加氢裂化装料的方法，其中：（a）在第一反应区中使氢气与与催化剂1接触的电荷反应，所述催化剂1包含至少一种基于氧化铝的基体和 至少一种氢脱氢组分; （b）来自第一反应区的流出物与第二反应区中的催化剂2接触，所述催化剂2包含：至少一种基质的20至97重量％; 3至80重量％的至少一种氢形式的Y沸石，所述沸石的特征在于SiO 2 / Al 2 O 3摩尔比超过4.5:1，钠含量小于1重量％，在沸石上煅烧 1100℃。 元素网的ao晶体参数小于24.70x10-10 m; 并且通过BET法测定的比表面积超过400m 2·g -1; 和至少一种氢脱氢组分。

    Hydroisomerization treatment process for feeds from the fisher-tropsch process
    4.
    发明授权
    Hydroisomerization treatment process for feeds from the fisher-tropsch process 失效
    来自渔草过程的饲料的加氢异构化处理过程

    公开(公告)号：US5834522A

    公开(公告)日：1998-11-10

    申请号：US553654

    申请日：1996-07-05

    申请人： Samuel Mignard ,  Nathalie Marchal ,  Slavik Kasztelan ,  Pierre-Henri Bigeard ,  Alain Billon

    发明人： Samuel Mignard ,  Nathalie Marchal ,  Slavik Kasztelan ,  Pierre-Henri Bigeard ,  Alain Billon

    IPC分类号： B01J21/08 ,  B01J21/12 ,  B01J23/40 ,  B01J35/10 ,  C10G45/40 ,  C10G45/62 ,  C07C27/00

    CPC分类号： C10G45/62 ,  B01J21/12 ,  B01J23/40 ,  B01J35/10 ,  B01J35/1019 ,  B01J35/1042 ,  B01J35/1057 ,  B01J35/1061 ,  B01J35/108

    摘要： The invention concerns a process for the hydroisomerisation treatment for feeds from the Fischer-Tropsch process. The catalyst is essentially constituted by 0.05% to 10% by weight of a precious metal and a silica (5-70%)/alumina support with a specific surface area of 100-500 m.sup.2 /g. The catalyst has an average pore diameter of 1-12 nm, the pore volume of pores with diameters between the average diameter .+-.3 nm being more than 40% of the total pore volume. The dispersion of the precious metal is 20-100% and the distribution coefficient for the precious metal is greater than 0.1. The process is operated at 200.degree.-450.degree. C. at a partial pressure of hydrogen of 2 to 25 MPa with a VVH of 0.1-10 h.sup.-1 and a hydrogen/feed volume ratio of 100-2000.

    摘要翻译： PCT No.PCT / FR95 / 00353 Sec。 371日期：1996年7月5日第 102（e）日期1996年7月5日PCT 1995年3月22日PCT公布。 出版物WO95 / 27020 PCT 日期1995年10月12日本发明涉及从费 - 托方法进料的加氢异构化处理方法。 催化剂基本上由0.05％至10％重量的贵金属和二氧化硅（5-70％）/比表面积为100-500m2 / g的氧化铝载体构成。 催化剂的平均孔径为1-12nm，直径在±3nm之间的孔的孔体积大于总孔体积的40％。 贵金属的分散度为20-100％，贵金属的分布系数大于0.1。 该工艺在200〜-450℃，氢气分压为2〜25MPa，VVH为0.1-10h-1，氢/进料体积比为100〜2000。

    Process for the improved production of middle distillates jointly with the production of high viscosity oils with high viscosity indices from heavy petroleum cuts
    6.
    发明授权
    Process for the improved production of middle distillates jointly with the production of high viscosity oils with high viscosity indices from heavy petroleum cuts 失效
    与重馏油高粘度指数的高粘度油生产联合生产中间馏分油的方法

    公开(公告)号：US5525209A

    公开(公告)日：1996-06-11

    申请号：US330820

    申请日：1994-10-24

    申请人： Alain Billon ,  Jean-Pierre Peries ,  Pierre-Henri Bigeard

    发明人： Alain Billon ,  Jean-Pierre Peries ,  Pierre-Henri Bigeard

    IPC分类号： B01J23/85 ,  B01J29/16 ,  C10G45/08 ,  C10G45/50 ,  C10G47/20 ,  C10G49/04 ,  C10G49/08 ,  C10G65/12 ,  C10G65/18

    CPC分类号： C10G65/12

    摘要： A process for the joint production of middle distillates and oil bases (viscosity index between 95 and 150) particularly from vacuum distillates and/or deasphalted oils, comprises a first step in which the feedstock is brought into contact with an amorphous catalyst containing at least one metal or metallic compound with a hydro-dehydrogenating function, such as Ni, Mo, W or Co, at a temperature of between 350.degree. C. and 430.degree. C., a pressure of between 5 and 20 MPa, a space velocity of between 0.1 and 5 h.sup.-1 in the presence of hydrogen in a ratio H.sub.2 /HC of 150 to 2,000 by volume. The product from the first step is brought into contact in a second step with a second catalyst comprising a support, a Y zeolite, at least one group VIB element and at least one group VIII metal at a temperature of between 350.degree. C. and 430.degree. C., a pressure of between 5 and 20 MPa and a space velocity of between 0.1 and 5 h.sup.-1.

    摘要翻译： 中间馏分和油基（尤其是真空馏分油和/或脱沥青油）粘度指数在95至150之间的联合生产方法包括第一步，其中原料与含有至少一种 具有氢脱氢功能的金属或金属化合物，例如Ni，Mo，W或Co，在350℃至430℃之间的温度下，压力为5至20MPa之间，空间速度介于 0.1和5h -1，在H 2 / HC比为150-2,000的氢存在下。 在第二步骤中，使第二催化剂在350℃和430℃之间的温度下与第二催化剂接触，所述第二催化剂包括载体，Y沸石，至少一种VIB族元素和至少一种VIII族金属 ℃，压力为5〜20MPa，空速为0.1〜5h -1。

    Process for converting heavy petroleum fractions that comprise a distillation stage, ebullated-bed hydroconversion stages of the vacuum distillate, and a vacuum residue and a catalytic cracking stage
    9.
    发明授权
    Process for converting heavy petroleum fractions that comprise a distillation stage, ebullated-bed hydroconversion stages of the vacuum distillate, and a vacuum residue and a catalytic cracking stage 有权
    用于转化包含蒸馏阶段，真空馏出物的沸腾床加氢转化阶段的重质石油馏分和减压渣油和催化裂解阶段的方法

    公开(公告)号：US06280606B1

    公开(公告)日：2001-08-28

    申请号：US09273486

    申请日：1999-03-22

    申请人： Frédéric Morel ,  Jean-Luc Duplan ,  Alain Billon ,  Stéphane Kressmann

    发明人： Frédéric Morel ,  Jean-Luc Duplan ,  Alain Billon ,  Stéphane Kressmann

    IPC分类号： C10G4700

    CPC分类号： C10G65/16 ,  C10G67/00

    摘要： Process for converting a hydrocarbon fraction that is obtained from atmospheric distillation of a crude, comprising a vacuum distillation stage (a) of said feedstock that makes it possible to obtain a vacuum distillate and a vacuum residue; a stage b) for treating at least a portion of the vacuum distillate in the presence of hydrogen; a stage c) for treating at least a portion of the vacuum residue in the presence of hydrogen, whereby said stages b) and c) are each carried out in at least one separate triphase reactor that contains at least one ebullated-bed hydrotreatment catalyst that operates with an upward flow of liquid and gas; a stage d) in which at least a portion of the product that is obtained in stage b) is sent to an atmospheric distillation zone from which a light fraction and a heavier liquid fraction are recovered; a stage e) in which at least a portion of the product that is obtained in stage c) is sent to an atmospheric distillation zone from which a light fraction and a heavier liquid fraction are recovered; and optionally a catalytic cracking stage f) in which at least a portion of the heavier liquid fractions that are obtained in stages d) and e) are at least partially cracked into lighter fuel-type fractions.

    摘要翻译： 用于转化由原油的常压蒸馏获得的烃馏分的方法，该粗产物包括能够获得真空馏分和减压渣油的所述原料的真空蒸馏阶段（a） 一个阶段b）用于在氢的存在下处理至少一部分真空馏出物; 阶段c）用于在氢存在下处理至少一部分真空残渣，其中所述阶段b）和c）各自在至少一个分离的三相反应器中进行，所述三相反应器含有至少一种沸腾床加氢处理催化剂， 以向上流动的液体和气体运行; 阶段d），其中将在阶段b）中获得的产品的至少一部分送至常压蒸馏区，从该馏分回收轻馏分和较重液体馏分; 阶段e），其中将在阶段c）中获得的产品的至少一部分送至常压蒸馏区，回收轻馏分和较重液体馏分; 和任选的催化裂化阶段f），其中在阶段d）和e）中获得的至少一部分较重的液体馏分至少部分地裂解成更轻的燃料型馏分。

    Hydroconversion of vacuum distillates and deasphalted oils in fixed beds and boiling beds
    10.
    发明授权
    Hydroconversion of vacuum distillates and deasphalted oils in fixed beds and boiling beds 失效
    在固定床和沸腾床中加氢转化真空蒸馏器和脱沥青油

    公开(公告)号：US06171477B2

    公开(公告)日：2001-01-09

    申请号：US09093808

    申请日：1998-06-09

    申请人： Fr{acute over (e)}d{acute over (e)}ric Morel ,  Jean-Luc Duplan ,  Alain Billon ,  St{acute over (e)}phane Kressmann

    发明人： Fr{acute over (e)}d{acute over (e)}ric Morel ,  Jean-Luc Duplan ,  Alain Billon ,  St{acute over (e)}phane Kressmann

    IPC分类号： C10G6500

    CPC分类号： C10G65/12 ,  C10G2300/107 ,  C10G2300/1074 ,  C10G2300/1077 ,  C10G2300/202 ,  C10G2300/206 ,  C10G2300/301 ,  C10G2300/4018 ,  C10G2300/4081 ,  C10G2300/44 ,  C10G2400/02 ,  C10G2400/04

    摘要： A process for the conversion of a hydrocarbon fraction comprising a step a) for treating a hydrocarbon charge in the presence of hydrogen in at least one reactor containing at least one hydrodesulphurisation catalyst in a fixed bed under conditions that make it possible to obtain a liquid effluent with a reduced sulphur content, a step b) for treating at least a part of the liquid effluent originating from step a) in the presence of hydrogen in at least one three-phase reactor, containing at least one hydrotreatment catalyst in a boiling bed, operating with an ascending stream of liquid and gas, said reactor comprising at least one means of withdrawing the catalyst from said reactor situated near the bottom of the reactor and at least one means of making up fresh catalyst in said reactor situated near the top of said reactor, and a step c) in which at least part of the product obtained in step b) is passed to a distillation zone from which are recovered a gas fraction, a motor fuel fraction of the petrol type, a motor fuel fraction of the diesel type, and a liquid fraction which is heavier than the diesel type fraction. This process may also contain a step d) for the catalytic cracking of the heavy fraction obtained in step c).

    摘要翻译： 一种用于烃馏分转化的方法，该方法包括步骤a），用于在固定床中在含有至少一种加氢脱硫催化剂的至少一个反应器中在氢气存在下处理烃装料，使得可以获得液体流出物 具有降低的硫含量，步骤b）用于在至少一个在沸腾床中含有至少一种加氢处理催化剂的三相反应器中在氢气存在下处理来自步骤a）的至少一部分液体流出物， 所述反应器包括至少一种将所述催化剂从位于所述反应器底部附近的所述反应器中排出的装置和至少一种在所述反应器中的新鲜催化剂的装置，所述装置位于所述反应器的顶部附近 反应器和步骤c），其中将步骤b）中获得的至少部分产物通入蒸馏区，从蒸馏区回收气体馏分，汽油燃料 汽油类型，柴油类型的机动车燃料部分和比柴油级分重的液体馏分。 该方法还可以包含步骤d）用于步骤c）中获得的重馏分的催化裂化。