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    Process for selectively producing C3 olefins in a fluid catalytic cracking process
    3.
    发明授权
    Process for selectively producing C3 olefins in a fluid catalytic cracking process 失效
    在流化催化裂化过程中选择性生产C3烯烃的方法

    公开(公告)号：US6093867A

    公开(公告)日：2000-07-25

    申请号：US73083

    申请日：1998-05-05

    申请人： Paul K. Ladwig ,  John Ernest Asplin ,  Gordon F. Stuntz ,  Tan-Jen Chen

    发明人： Paul K. Ladwig ,  John Ernest Asplin ,  Gordon F. Stuntz ,  Tan-Jen Chen

    IPC分类号： C07C4/02 ,  C07C4/06 ,  C07C11/02 ,  C10G11/02 ,  C10G11/04 ,  C10G11/05 ,  C10G57/02

    CPC分类号： C10G57/02 ,  C10G2400/20

    摘要： A process for selectively producing C.sub.3 olefins from a catalytically cracked or thermally cracked naphtha stream. The naphtha stream is introduced into a process unit comprised of a reaction zone, a stripping zone, a catalyst regeneration zone, and a fractionation zone. The naphtha feedstream is contacted in the reaction zone with a catalyst containing from about 10 to 50 wt. % of a crystalline zeolite having an average pore diameter less than about 0.7 nanometers at reaction conditions which include temperatures ranging from about 500.degree. to 650.degree. C. and a hydrocarbon partial pressure from about 10 to 40 psia. Vapor products are collected overhead and the catalyst particles are passed through the stripping zone on the way to the catalyst regeneration zone. Volatiles are stripped with steam in the stripping zone and the catalyst particles are sent to the catalyst regeneration zone where coke is burned from the catalyst, which is then recycled to the reaction zone. Overhead products from the reaction zone are passed to a fractionation zone where a stream of C.sub.3 's is recovered and a stream rich in C.sub.4 and/or C.sub.5 olefins is recycled to the stripping zone.

    摘要翻译： 从催化裂化或热裂解的石脑油流中选择性生产C3烯烃的方法。 将石脑油流引入由反应区，汽提区，催化剂再生区和分馏区构成的工艺单元中。 石脑油原料流在反应区中与含有约10至50wt。 ％的平均孔径小于约0.7纳米的结晶沸石在包括约500℃至650℃的温度和约10至40psia的烃分压的反应条件下进行。 蒸气产物被顶部收集，催化剂颗粒在通向催化剂再生区的途中通过汽提区。 挥发物在汽提区中用蒸汽汽提，并将催化剂颗粒送入催化剂再生区，其中焦炭从催化剂燃烧，然后再循环到反应区。 来自反应区的高架物质被送入分馏区，其中回收C3的物流，富含C4和/或C5烯烃的物流被循环到汽提区。

    Process for producing polypropylene from C3 olefins selectively produced in a fluid catalytic cracking process
    4.
    发明授权
    Process for producing polypropylene from C3 olefins selectively produced in a fluid catalytic cracking process 失效
    在流化催化裂化过程中选择性生产的C3烯烃生产聚丙烯的方法

    公开(公告)号：US06388152B1

    公开(公告)日：2002-05-14

    申请号：US09517554

    申请日：2000-03-02

    申请人： Paul K. Ladwig ,  John E. Asplin ,  Gordon F. Stuntz ,  Tan-Jen Chen

    发明人： Paul K. Ladwig ,  John E. Asplin ,  Gordon F. Stuntz ,  Tan-Jen Chen

    IPC分类号： C07C406

    CPC分类号： C10G57/02 ,  C10G2400/20

    摘要： A process for producing polymers from olefins selectively produced from a catalytically cracked or thermally cracked naphtha stream is disclosed herein. The naphtha stream is introduced into a process unit comprised of a reaction zone, a stripping zone, a catalyst regeneration zone, and a fractionation zone. The naphtha feedstream is contacted in the reaction zone with a catalyst containing from about 10 to 50 wt. % of a crystalline zeolite having an average pore diameter less than about 0.7 nanometers at reaction conditions which include temperatures ranging from about 500° to 650° C. and a hydrocarbon partial pressure from about 10 to 40 psia. Vapor products are collected overhead and the catalyst particles are passed through the stripping zone on the way to the catalyst regeneration zone. Volatiles are stripped with steam in the stripping zone and the catalyst particles are sent to the catalyst regeneration zone where coke is burned from the catalyst, which is then recycled to the reaction zone. Overhead products from the reaction zone are passed to a fractionation zone where a stream of C3 products is recovered and a stream rich in C4 and/or C5 olefins is recycled to the stripping zone. The olefins can be further processed and polymerized to form a variety of polymer materials.

    摘要翻译： 本文公开了从由催化裂化或热裂解的石脑油流选择性地生产的烯烃生产聚合物的方法。 将石脑油流引入由反应区，汽提区，催化剂再生区和分馏区构成的工艺单元中。 石脑油原料流在反应区中与含有约10至50wt。 在包括约500℃至650℃的温度和约10至40psia的烃分压的反应条件下具有平均孔径小于约0.7纳米的结晶沸石的％。 蒸气产物被顶部收集，催化剂颗粒在通向催化剂再生区的途中通过汽提区。 挥发物在汽提区中用蒸汽汽提，并将催化剂颗粒送入催化剂再生区，其中焦炭从催化剂燃烧，然后再循环到反应区。 来自反应区的开销产物被送入分馏区，其中回收C3产物流，并且将富含C4和/或C5烯烃的物流再循环到汽提区。 烯烃可以进一步加工和聚合以形成各种聚合物材料。

    Process for producing polypropylene from C3 olefins selectively produced by a two stage fluid catalytic cracking process
    7.
    发明授权
    Process for producing polypropylene from C3 olefins selectively produced by a two stage fluid catalytic cracking process 失效
    通过两阶段流化催化裂化方法选择性生产的C3烯烃生产聚丙烯的方法

    公开(公告)号：US06258257B1

    公开(公告)日：2001-07-10

    申请号：US09517551

    申请日：2000-03-02

    申请人： George A. Swan, III ,  Michael W. Bedell ,  Paul K. Ladwig ,  John E. Asplin ,  Gordon F. Stuntz ,  William A. Wachter ,  B. Erik Henry

    发明人： George A. Swan, III ,  Michael W. Bedell ,  Paul K. Ladwig ,  John E. Asplin ,  Gordon F. Stuntz ,  William A. Wachter ,  B. Erik Henry

    IPC分类号： C10G5102

    CPC分类号： C10G57/02 ,  C10G2400/20

    摘要： A process for producing polymers from olefins selectively produced by a two stage process for selectively producing C2 to C4 olefins from a gas oil or resid is disclosed herein. The gas oil or resid is reacted in a first stage comprising a fluid catalytic cracking unit wherein it is converted in the presence of conventional large pore zeolitic catalyst to reaction products, including a naphtha boiling range stream. The naphtha boiling range stream is introduced into a second stage comprising a process unit containing a reaction zone, a stripping zone, a catalyst regeneration zone, and a fractionation zone. The naphtha feed is contacted in the reaction zone with a catalyst containing from about 10 to 50 wt. % of a crystalline zeolite having an average pore diameter less than about 0.7 nanometers at reaction conditions which include temperatures ranging from about 500 to 650° C. and a hydrocarbon partial pressure from about 10 to 40 psia. Vapor products are collected overhead and the catalyst particles are passed through the stripping zone on the way to the catalyst regeneration zone. Volatiles are stripped with steam in the stripping zone and the catalyst particles are sent to the catalyst regeneration zone where coke is burned from the catalyst, which is then recycled to the reaction zone.

    摘要翻译： 本文公开了一种通过二级方法选择性制备聚合物的方法，用于从瓦斯油或渣油中选择性地生产C2至C4烯烃。 瓦斯油或渣油在包括流化催化裂化装置的第一阶段中反应，其中在常规大孔沸石催化剂存在下将其转化为包括石脑油沸程的反应产物。 将石脑油沸程流引入包含含有反应区，汽提区，催化剂再生区和分馏区的处理单元的第二阶段。 石脑油进料在反应区中与含有约10至50wt。 在包括约500至650℃的温度和约10至40psia的烃分压的反应条件下具有平均孔径小于约0.7纳米的结晶沸石的百分比。 蒸气产物被顶部收集，催化剂颗粒在通向催化剂再生区的途中通过汽提区。 挥发物在汽提区中用蒸汽汽提，并将催化剂颗粒送入催化剂再生区，其中焦炭从催化剂燃烧，然后再循环到反应区。

    Two stage fluid catalytic cracking process for selectively producing b. C.su2 to C.sub.4 olefins
    9.
    发明授权
    Two stage fluid catalytic cracking process for selectively producing b. C.su2 to C.sub.4 olefins 失效
    用于选择性生产C2至C4烯烃的两阶段流化催化裂解方法

    公开(公告)号：US6106697A

    公开(公告)日：2000-08-22

    申请号：US073084

    申请日：1998-05-05

    申请人： George A. Swan ,  Michael W. Bedell ,  Paul K. Ladwig ,  John E. Asplin ,  Gordon F. Stuntz ,  William A. Wachter ,  Brian Erik Henry

    发明人： George A. Swan ,  Michael W. Bedell ,  Paul K. Ladwig ,  John E. Asplin ,  Gordon F. Stuntz ,  William A. Wachter ,  Brian Erik Henry

    IPC分类号： C10G11/05 ,  C10G51/02 ,  C10G57/00 ,  C10G57/02

    CPC分类号： C10G57/02 ,  C10G2400/20

    摘要： C.sub.2 to C.sub.4 olefins are selectively produced from a gas oil or resid in a two stage process. The gas oil or resid is reacted in a first stage comprised of a fluid catalytic cracking unit wherein it is converted in the presence of conventional large pore zeolitic catalyst to reaction products, including a naphtha boiling range stream. The naphtha boiling range stream is introduced into a second stage comprised of a process unit containing a reaction zone, a stripping zone, a catalyst regeneration zone, and a fractionation zone. The naphtha feedstream is contacted in the reaction zone with a catalyst containing from about 10 to 50 wt. % of a crystalline zeolite having an average pore diameter less than about 0.7 nanometers at reaction conditions which include temperatures ranging from about 500 to 650.degree. C. and a hydrocarbon partial pressure from about 10 to 40 psia. Vapor products are collected overhead and the catalyst particles are passed through the stripping zone on the way to the catalyst regeneration zone. Volatiles are stripped with steam in the stripping zone and the catalyst particles are sent to the catalyst regeneration zone where coke is burned from the catalyst, which is then recycled to the reaction zone.

    摘要翻译： C 2 -C 4烯烃可以从瓦斯油中选择性地制备，或者在两段工艺中残留。 瓦斯油或渣油在由流化催化裂化装置组成的第一阶段中反应，其中在常规大孔沸石催化剂存在下将其转化为包括石脑油沸程的反应产物。 将石脑油沸程流引入包含含有反应区，汽提区，催化剂再生区和分馏区的处理单元的第二阶段。 石脑油原料流在反应区中与含有约10至50wt。 ％的平均孔径小于约0.7纳米的结晶沸石在包括约500至650℃的温度和约10至40psia的烃分压的反应条件下进行。 蒸气产物被顶部收集，催化剂颗粒在通向催化剂再生区的途中通过汽提区。 挥发物在汽提区中用蒸汽汽提，并将催化剂颗粒送入催化剂再生区，其中焦炭从催化剂燃烧，然后再循环到反应区。