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    • 73. 发明授权
    • Process and system for the dry quenching of coke
    • 焦炭干法淬火的工艺和系统
    • US4627174A
    • 1986-12-09
    • US725048
    • 1985-04-19
    • Kurt HeddenKurt-Gunther BeckWolfgang RohdeHorst Schumacher
    • Kurt HeddenKurt-Gunther BeckWolfgang RohdeHorst Schumacher
    • C10B39/02C10B57/10F26B3/16
    • C10B57/10C10B39/02
    • Glowing coke descending through a cooling duct in a coking plant is quenched by two gas flows respectively traversing an upper compartment and a lower compartment of the duct, the two compartments meeting at a restricted gate for the passage of the coke. At least the lower gas flow, passing in countercurrent to the descending coke charge, is also circulated through a drying and preheating oven for coal to be fed to a coke-oven battery of the plant, thus containing some water vapor. When the upper flow is also constituted by coal-drying gas, it is passed downward through the upper compartment in order to reduce the height of a high-temperature zone in which combustion and thus loss of coke could occur. The coke gate is formed by a funnel-shaped upper partition and an upwardly pointing conical lower partition between which a scavenger gas passes in cross-flow.
    • 通过焦化装置中的冷却管道下降的发光焦炭通过分别穿过管道的上隔室和下隔室的两个气流骤冷,两个隔室在限制门处会合以供焦炭通过。 至少与下降焦炭装置逆流通过的较低气体流量也通过干燥和预热炉循环,以将煤供给到设备的焦炉电池,从而含有一些水蒸汽。 当上部流动也由干燥气体构成时,其通过上部区域向下通过,以便降低可能发生燃烧和因此可能发生焦炭的高温区域的高度。 焦炭门由漏斗形的上部隔板和向上指向的圆锥形下部隔板形成,在该隔板中,清除剂气体在其间交叉流动。
    • 74. 发明授权
    • Process for drying coal in two-stage flow-through circulation heaters
    • 在两级流通循环加热器中干燥煤的工艺
    • US4174946A
    • 1979-11-20
    • US829254
    • 1977-08-30
    • Wolfgang Rohde
    • Wolfgang Rohde
    • F27B15/00C10B57/08C10B57/10F23G5/30F26B3/10F26B17/10F26B23/02
    • C10B57/08F26B17/101F26B23/02
    • Coal is dried by passing it successively to two tubular flow-through circulation heating elements together with a heat carrier gas, withdrawing the partially dried coal emanating from the first heating element and passing it into the inlet end of the second heating element and recovering the substantially dry coal from the gas and coal mass emanating from the second heating element, the hot vapors received from the outlet end of the first heating element being recirculated after mixing them with fresh combustion gases into the second heating element and the heat carrier gas emanating from the second heating element after separation of the coal therefrom being passed after mixing with fresh combustion gases into the first heating element.
    • 将煤通过依次通过两个管状流通循环加热元件与热载气一起干燥,从第一加热元件排出部分干燥的煤,并将其通入第二加热元件的入口端并回收基本上 从第二加热元件发出的来自气体和煤质量的干煤,从第一加热元件的出口端接收的热蒸汽在将它们与新鲜燃烧气体混合到第二加热元件中之后再循环,并且从第一加热元件发出的热载气 在与新鲜燃烧气体混合进入第一加热元件之后,将煤分离后的第二加热元件通过。
    • 80. 发明申请
    • PROCESS FOR PREPARING ISOPROPANOL AND 2-BUTANOL FROM THE CORRESPONDING ALKANES
    • 从相应的碱中制备异丙醇和2-丁醇的方法
    • US20100048960A1
    • 2010-02-25
    • US12374351
    • 2007-07-16
    • Georg DegenSven CroneRalf BoehlingAnsgar Gereon AltenhoffWolfgang RohdeJochen BuerkleGoetz-Peter SchindlerThomas HoltmannMarkus Schmitt
    • Georg DegenSven CroneRalf BoehlingAnsgar Gereon AltenhoffWolfgang RohdeJochen BuerkleGoetz-Peter SchindlerThomas HoltmannMarkus Schmitt
    • C07C29/04
    • C07C67/04C07C29/095Y02P20/127C07C31/10C07C31/12C07C69/06C07C69/14
    • A process for preparing alkanols (I) selected from the group consisting of isopropanol and 2-butanol from the corresponding alkanes (II) selected from the group consisting of propane and n-butane, comprising the steps of: A) providing a starting gas stream a comprising the alkane (II); B) feeding the starting gas stream a comprising the alkane (II) into a dehydrogenation zone and subjecting the alkane (II) to a dehydrogenation to the alkene (III) to obtain a product gas stream b comprising the alkene (III) and unconverted alkane (II), with or without high boilers, steam, hydrogen and low boilers; C) at least compressing product gas stream b, optionally separating product gas stream b into an aqueous phase c1, a phase c2 comprising the alkene (III) and the alkane (II), with or without high boilers, and a gas phase c3 comprising hydrogen and low boilers; D) reacting product gas stream b or the phase c2 comprising alkene (III) and alkane (II) with an organic acid (IV) in an esterification zone to obtain a product mixture d comprising the corresponding alkyl ester (V) of the organic acid and the unconverted alkane (II); E) removing from product mixture d a gas stream e1 which comprises an alkane (II) and is recycled into the dehydrogenation zone if appropriate, and a product mixture e2 comprising the alkyl ester; F) reacting the product mixture e2 comprising the alkyl ester with water in an ester hydrolysis zone to give a product mixture f comprising the alkanol (I) and the organic acid (IV); G) removing the alkanol (I) and the organic acid (IV) from product mixture f and, if appropriate, recycling the organic acid into the esterification zone.
    • 从选自丙烷和正丁烷的相应的烷烃(II)制备选自异丙醇和2-丁醇的链烷醇(I)的方法,包括以下步骤:A)提供起始气流 a包含烷烃(II); B)将包含烷烃(II)的起始气体流(a)进料到脱氢区中并使烷烃(II)脱氢至烯烃(III),得到包含烯烃(III)和未转化烷烃的产物气流b (II),有或没有高锅炉,蒸汽,氢气和低锅炉; C)至少压缩产物气流b,任选地将产物气流b分离成水相c1,包含烯烃(III)和烷烃(II)的阶段c2,具有或不具有高锅炉,以及气相c3,其包含 氢和低锅炉; D)使产物气流b或包含烯烃(III)和烷烃(II)的相c与酯化区中的有机酸(IV)反应,得到包含相应的有机酸烷基酯(V)的产物混合物d 和未转化的烷烃(II); E)从产物混合物d除去包含烷烃(II)的气流e1,并且如果合适的话再循环到脱氢区中,以及包含烷基酯的产物混合物e2; F)在酯水解区中使包含烷基酯的产物混合物e2与水反应,得到包含链烷醇(I)和有机酸(IV)的产物混合物f; G)从产物混合物f中除去链烷醇(I)和有机酸(IV),如果合适,将有机酸再循环到酯化区。