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    • 31. 发明申请
    • PROCESS FOR THE CO-PRODUCTION OF A STREAM OF A FATTY ALCOHOL HAVING A FIRST CARBON CHAIN LENGTH AND A STREAM OF A FATTY ALCOHOL HAVING A SECOND CARBON LENGTH
    • US20120016163A1
    • 2012-01-19
    • US13061904
    • 2010-03-30
    • Donald Hugh McKinleyAndrew George HilesRikard Umberto AnderssonJohn Richard Hensman
    • Donald Hugh McKinleyAndrew George HilesRikard Umberto AnderssonJohn Richard Hensman
    • C07C29/149
    • C07C29/149Y02P20/132C07C31/125
    • A process for the co-production of a stream of a fatty alcohol having first carbon chain lengths and a stream of a fatty alcohol having a second carbon chain lengths, said second carbon chain lengths being longer than said first carbon chain lengths, said process comprising the steps of: (a) supplying a stream comprising lower alkyl esters of fatty acids having chain lengths comprising the first and second chain lengths to a first vaporisation zone and contacting said stream with an amount of hydrogen recycled from step (i) which is sufficient to vaporise the lower alkyl esters of the fatty acids having the first carbon chain lengths into the hydrogen; (b) supplying the hydrogen and the vaporised lower alkyl esters of fatty acids having the first carbon chain lengths to a first reaction zone comprising catalyst and operating under reaction conditions to allow hydrogenation to the desired alcohol having first carbon chain lengths; (c) recovering from the first reaction zone an alcohol product stream having first carbon chain lengths and the hydrogen; (d) supplying the unvaporised lower alkyl esters of the fatty acids having second carbon chain lengths remaining from step (a) to a second vaporisation zone; (e) contacting the unvaporised lower alkyl esters having second carbon chain lengths in the second vaporisation zone with an amount of hydrogen sufficient to vaporise the lower alkyl esters having fatty acids of the second carbon chain lengths into the hydrogen; (f) supplying the hydrogen and the vaporised lower alkyl esters of fatty acids having second carbon chain lengths to a second reaction zone comprising catalyst and operating under reaction conditions to allow hydrogenation to the desired alcohol having second carbon chain lengths; (g) recovering from the second reaction zone an alcohol product stream having second carbon chain lengths and hydrogen; (h) separating the stream of fatty acid alcohol having the second carbon chain length from hydrogen; and (i) recycling a portion of the hydrogen recovered in step (h) to the first vaporisation zone and a portion to the second vapourisation zone.
    • 33. 发明申请
    • Process for the Preparation of N-Alkyl Pyrrolidones
    • N-烷基吡咯烷酮的制备方法
    • US20070270596A1
    • 2007-11-22
    • US11570179
    • 2005-06-01
    • John HensmanRiyaz Khambati
    • John HensmanRiyaz Khambati
    • C07D207/267
    • C07D207/267
    • A process for the production of N-alkylpyrrolidone from γ-butyrolactone and monoalkylamine in the liquid phase comprising the steps of: feeding monoalkylamine and γ-butyrolactone, in the absence of water or in the presence of less than about 1 wt % of water, to a reaction zone to form a reaction mixture; heating the reaction mixture; withdrawing a product stream from the reaction zone and passing the stream to a distillation zone comprising at least one distillation column operated at sub-atmospheric pressure; adding water to the distillation zone; isolating at least one overhead stream from the distillation zone comprising monoalkylamine, water and optionally N-alkyl-pyrrolidone and condensing the overhead stream against cooling water.
    • 在液相中从γ-丁内酯和单烷基胺生产N-烷基吡咯烷酮的方法,包括以下步骤:在不存在水的情况下或在少于约1重量%的水的存在下加入单烷基胺和γ-丁内酯, 反应区形成反应混合物; 加热反应混合物; 从反应区抽出产物流并将物流送至包含至少一个在低于大气压的压力下运行的蒸馏塔的蒸馏区; 向蒸馏区加水; 从包含单烷基胺,水和任选的N-烷基 - 吡咯烷酮的蒸馏区分离至少一个塔顶物流,并将塔顶馏出物与冷却水冷凝。
    • 35. 发明授权
    • Hydroformylation process with recycle of active rhodium catalyst
    • 加氢甲酰化工艺与活性铑催化剂循环
    • US06946580B2
    • 2005-09-20
    • US10479309
    • 2002-05-29
    • James Andrew BanisterGeorge Edwin Harrison
    • James Andrew BanisterGeorge Edwin Harrison
    • B01J31/24B01J31/40B01J38/00B01J38/04B01J38/12C07B61/00C07C45/50C07C47/02
    • C07C45/50Y02P20/584C07C47/02
    • The present invention relates to a continuous hydroformylation process for the production of an aldehyde by hydroformylation of an olefin which comprises: providing a hydroformylation zone containing a charge of a liquid reaction medium having dissolved therein a rhodium hydroformylation catalyst comprising rhodium in combination with carbon monoxide and a ligand; supplying the olefin to the hydroformylation zone; maintaining temperature and pressure conditions in the hydroformylation zone conducive to hydroformylation of the olefin; recovering from the liquid hydroformylation medium a hydroformylation product comprising aldehyde; recovering from the hydroformylation zone a stream comprising the rhodium catalyst; contacting at least a portion of the stream with a solid acidic absorbent under process conditions which allow at least some of the rhodium to become bound to the absorbent; subjecting the rhodium bound to the absorbent, under process conditions which allow desorption of the metal, to a fluid stripping medium comprising hydrogen and solvent; recovering the rhodium hydride catalyst; and recycling the rhodium hydride catalyst to the hydroformylation zone.
    • 本发明涉及通过烯烃的加氢甲酰化生产醛的连续加氢甲酰化方法,该方法包括:提供含有液体反应介质的加氢甲酰化区,该液体反应介质溶解有铑加氢甲酰化催化剂,该催化剂包含铑与一氧化碳和 配体; 将烯烃供应到加氢甲酰化区; 维持加氢甲酰化区中有利于烯烃加氢甲酰化的温度和压力条件; 从液体加氢甲酰化介质中回收含有醛的加氢甲酰化产物; 从加氢甲酰化区回收包含铑催化剂的物流; 在工艺条件下使至少一部分流与固体酸性吸收剂接触,使得至少一些铑与吸收剂结合; 在允许金属解吸的工艺条件下将结合到吸收剂上的铑经受包含氢和溶剂的流体汽提介质; 回收氢化铑催化剂; 并将氢化铑催化剂再循环到加氢甲酰化区。
    • 36. 发明授权
    • Process for the production of ethers, typically thf
    • 用于生产醚的方法,通常为
    • US06936727B2
    • 2005-08-30
    • US10483524
    • 2002-07-10
    • David Mark SuttonAndrew George HilesGraham ReedJohn Anthony Stannard
    • David Mark SuttonAndrew George HilesGraham ReedJohn Anthony Stannard
    • C07B61/00C07D307/08
    • C07D307/08
    • A process is described for the production of ethers, typically terahydrofuran, by reaction of a corresponding organic feed material selected from dicarboxylic acids and/or anhydrides, monoesters of dicarboxylic acids and/or anhydrides, diesters of dicarboxylic acids and/or anhydrides, lactones, and mixtures of two or more thereof in the presence of hydrogen which comprises the steps of: (a) supplying a stream comprising the organic feed material to a first vaporisation zone and contacting said feed with cycle gas comprising hydrogen such that at least a portion of the feed material is vaporised by and into the cycle gas; (b) supplying at least a portion of the cycle gas and the vaporised feed material to a first reaction zone comprising catalyst and operating under reaction conditions to allow hydrogenation and dehydration to occur; (c) recovering from the first reaction zone an intermediate product stream comprising unreacted feed material, cycle gas, desired product(s), and any co-products and by-products; (d) supplying the intermediate product stream to a second vaporisation zone and contacting it with additional feed material such that the said additional feed material is vaporised by and into the intermediate product stream; (e) supplying the product of step (d) to a subsequent reaction zone comprising catalyst and operating under reaction conditions to allow hydrogenation and, if required, dehydration to occur; and (f) recovering from the subsequent reaction zone a product stream comprising the ether.
    • 描述了通过相应的选自二羧酸和/或酸酐的有机原料,二羧酸和/或酸酐的单酯,二羧酸和/或酸酐的二酯,内酯, 和其中两种或更多种在氢存在下的混合物,其包括以下步骤:(a)将包含有机进料的物流供应到第一蒸发区,并使所述进料与包含氢的循环气体接触,使得至少一部分 原料被循环气体蒸发并进入循环气体中; (b)将循环气体和蒸发的进料的至少一部分供应到包含催化剂并在反应条件下操作以允许氢化和脱水发生的第一反应区; (c)从第一反应区回收包含未反应的进料,循环气体,所需产物和任何副产物和副产物的中间产物流; (d)将中间产物流供应到第二蒸发区并使其与另外的进料相接触,使得所述另外的进料通过中间产物流蒸发并进入中间产物流; (e)将步骤(d)的产物供给到包含催化剂的后续反应区域中,并在反应条件下操作以允许氢化,如果需要,进行脱水发生; 和(f)从后续反应区回收包含醚的产物流。
    • 37. 发明授权
    • Process for the commercial production of polyhydroxy alcohols and glycols
    • 用于商业生产多羟基醇和二醇的方法
    • US5841002A
    • 1998-11-24
    • US723186
    • 1996-09-27
    • George Edwin HarrisonArthur James Reason
    • George Edwin HarrisonArthur James Reason
    • C07C29/141C07C29/76C07C45/72C25B1/16C07C31/18
    • C25B1/16C07C29/141C07C29/76C07C45/72Y02P20/584
    • An aldolisation process is disclosed for converting an aldehyde or mixture of aldehydes, such as iso-butyraldehyde and formaldehyde, to a desired polyhydroxy alcohol or glycol, such as neopentyl glycol. Aldolisation is effected in a stirred tank reactor using an alkali catalyst, such as sodium hydroxide. An aldolisation intermediate product is converted to the desired polyhydroxy alcohol or glycol by a hydrogenation or cross-Cannizzaro reaction step. The product is recovered and an aqueous catalyst-containing phase is recycled to the aldolisation zone. At least a portion of this catalyst recycle stream is purged to control the build up of cross-Cannizzaro products in the recycle stream. The purge stream is treated electrolytically to obtain an aqueous catalyst-containing solution for recycle to the aldolisation zone and an effluent stream comprising volatile organic materials and being substantially free from alkali catalyst.
    • 公开了醛醛化方法,用于将醛或其混合物如异丁醛和甲醛转化成所需的多羟基醇或二醇,例如新戊二醇。 醛化在使用碱催化剂如氢氧化钠的搅拌釜反应器中进行。 醛化中间体产物通过氢化或交叉坎尼扎罗反应步骤转化成所需的多羟基醇或二醇。 回收产物并将含水催化剂的相循环到醛醇化区。 将该催化剂再循环料流的至少一部分清除以控制在再循环流中交叉的Cannizzaro产品的积累。 电解处理清洗流以获得用于循环到醛醇化区的含水催化剂的溶液和包含挥发性有机材料并基本上不含碱催化剂的流出物流。
    • 40. 发明申请
    • Fischer-Tropsch Process In A Radial Reactor
    • 径向反应器中的费 - 托工艺
    • US20140187653A1
    • 2014-07-03
    • US13579973
    • 2012-02-06
    • Timothy Douglas Gamlin
    • Timothy Douglas Gamlin
    • C07C1/04
    • C07C1/041B01J8/0214B01J8/0285B01J8/0415B01J8/067B01J19/2485B01J2208/00814B01J2219/00038B01J2219/0004C10G2/341
    • In a process for converting synthesis gas to higher hydrocarbons in a tubular reactor, reactants are introduced through an inlet of the reactor. The reactants are passed downwardly through at least one tube to an upper surface of a catalyst carrier where they pass into a passage defined by an inner perforated wall of a catalyst container before passing radially through the catalyst bed towards the perforated outer wall. Reaction occurs as the synthesis gas contacts the catalyst. Unreacted reactant and product is passed out of the container through a perforated outer wall thereof and then upwardly between a skirt and an outer wall of the container, followed by being directed over the end of the skirt and downwardly between the skirt and the reactor tube where heat transfer takes place. These steps are repeated for any subsequent catalyst carrier, then product is removed from an outlet of the reactor.
    • 在管式反应器中将合成气转化为高级烃的方法中,通过反应器的入口引入反应物。 反应物通过至少一个管子向下通过催化剂载体的上表面,在催化剂载体的上表面通过催化剂容器的内部穿孔壁限定的通道中,然后通过催化剂床朝向穿孔的外壁。 当合成气与催化剂接触时,会发生反应。 未反应的反应物和产物通过其穿孔的外壁从容器中穿过,然后在容器的裙部和外壁之间向上延伸,随后被引导到裙部的端部上并在裙部和反应器管之间向下 传热发生。 对于任何后续的催化剂载体重复这些步骤,然后从反应器的出口除去产物。