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    Process for the production of carbon molecular sieves
    2.
    发明授权
    Process for the production of carbon molecular sieves 失效
    碳分子筛生产工艺

    公开(公告)号：US5498589A

    公开(公告)日：1996-03-12

    申请号：US211207

    申请日：1994-03-21

    申请人： Hans-Jurgen Schroter ,  Heinrich Heimbach ,  Klaus-Dirk Henning ,  Karl Knoblauch ,  Alfons S.-S. Berndt ,  Ferdinand Tarnow

    发明人： Hans-Jurgen Schroter ,  Heinrich Heimbach ,  Klaus-Dirk Henning ,  Karl Knoblauch ,  Alfons S.-S. Berndt ,  Ferdinand Tarnow

    IPC分类号： B01J20/20

    CPC分类号： B01J20/20 ,  Y10S95/902

    摘要： A process is disclosed for preparing a carbon molecular sieve used for the separation of oxygen from nitrogen, which comprises the steps of:(a) milling hard coal to a grain size of 95%

    摘要翻译： PCT No.PCT / EP92 / 02275第 371日期1994年3月21日 102（e）1994年3月21日PCT提交1992年10月1日PCT公布。 公开号WO93 / 06920 公开了一种用于制备用于从氮气中分离氧的碳分子筛的方法，其包括以下步骤：（a）将硬煤研磨至95％<20μm的粒度; （b）在流化床中用空气氧化细磨的硬煤; （c）加入水和煤焦油沥青作为粘合剂，并将精细研磨的硬质煤成型; （d）在500〜850℃的温度下在回转窑中成形为细磨的硬质煤，在55〜65分钟的时间内进行碳化，得到堆积密度为 530至560g / l; （e）用蒸汽在900℃下活化碳化产物165至195分钟，得到堆积密度为590至650g / l的烧结碳质产品; 和（f）用碳分解碳氢化合物在750-850℃下处理烧结的碳质产物，得到所述碳分子筛。

    Adsorption-desorption process for the recovery of hydrogen
    4.
    发明授权
    Adsorption-desorption process for the recovery of hydrogen 失效
    用于回收氢的吸附 - 脱附过程

    公开(公告)号：US4432774A

    公开(公告)日：1984-02-21

    申请号：US93616

    申请日：1979-11-09

    申请人： Harald Juntgen ,  Karl Knoblauch ,  Jurgen Reichenberger ,  Hans-Jurgen Schroter

    发明人： Harald Juntgen ,  Karl Knoblauch ,  Jurgen Reichenberger ,  Hans-Jurgen Schroter

    IPC分类号： B01D53/04 ,  C01B3/56

    CPC分类号： C01B3/56 ,  C01B2203/043 ,  C01B2203/0465 ,  C01B2203/047 ,  C01B2203/0475 ,  C01B2203/048

    摘要： An adsorption-desorption process for the recovery of hydrogen from a feed gas containing trace pollutants adapted to be strongly adsorbed, in concentrations generally below 1% by volume and containing components adapted for only light adsorption, in concentrations above 1% by volume is operated through a preliminary first adsorption stage for the strongly adsorbable trace pollutants and a second main adsorption stage for the light adsorbable components and for the discharge of hydrogen. Contrary to the prior art where the adsorption-desorption was effected by alternating high pressure and low pressure cycles in the main adsorption stage only, the pressure cycles in the present case are carried out both in the preliminary first adsorption stage and in the second main adsorption stage, preferably by arranging the two adsorption states in series. The process substantially extends the service time of the adsorber used in the first adsorption stage.

    摘要翻译： 用于从含有高于1体积％浓度的适于强吸附的含有微量污染物的原料气中回收氢的吸附 - 脱附方法通常以低于1体积％并且仅含有轻吸附的成分浓度高于1体积％ 用于强吸附痕量污染物的初步第一吸附阶段和用于光吸附组分和氢排放的第二主要吸附阶段。 与仅在主吸附阶段交替的高压低压循环进行吸附解吸的现有技术相反，本例中的压力循环在初步第一吸附阶段和第二主吸附过程中进行 优选通过串联布置两个吸附状态。 该方法基本上延长了在第一吸附阶段中使用的吸附器的使用时间。

    Process for the enrichment of gases
    5.
    发明授权
    Process for the enrichment of gases 失效
    气体浓缩过程

    公开(公告)号：US4011065A

    公开(公告)日：1977-03-08

    申请号：US523687

    申请日：1974-11-14

    申请人： Heinrich Munzner ,  Heinrich Heimbach ,  Werner Korbacher ,  Werner Peters ,  Harald Juntgen ,  Karl Knoblauch ,  Dieter Zundorf

    发明人： Heinrich Munzner ,  Heinrich Heimbach ,  Werner Korbacher ,  Werner Peters ,  Harald Juntgen ,  Karl Knoblauch ,  Dieter Zundorf

    IPC分类号： B01D53/04 ,  C01B13/02 ,  B01D15/06

    CPC分类号： B01D53/0423 ,  B01D53/04 ,  C01B13/0266 ,  B01D2253/102 ,  B01D2256/12 ,  B01D2259/402 ,  B01D53/0446 ,  C01B2210/0046

    摘要： An initial gaseous mixture of at least two components is passed through an adsorber which preferentially adsorbs one of the components. This initially loads the adsorber. Subsequently, another gaseous mixture, having a greater concentration of the preferentially adsorbed component than the initial gaseous mixture, is passed through the adsorber so as to additionally load the adsorber. Part of the gas in the adsorber is then removed. This initially unloads the adsorber and yields a first fraction containing both components with the concentration of the preferentially adsorbed component being greater than that in the initial gaseous mixture. Subsequently, part of the gas still remaining in the adsorber is removed so as to further unload the adsorber. This results in a second fraction including both components and wherein the concentration of the preferentially adsorbed component is greater than that in both the second gaseous mixture to be passed through the adsorber and the first fraction removed from the adsorber. Finally, the remainder of the gas in the adsorber is removed so as to completely unload the adsorber. This yields a third fraction including both components with the concentration of the preferentially adsorbed component being lower than that in the second fraction removed from the adsorber but greater than that in the initial gaseous mixture passed into the adsorber. The first and third fractions may be used for additionally loading the adsorber in a subsequent cycle. A preferred application is the enrichment of oxygen-containing gases, particularly air, which include a component of greater molecular size than oxygen. A preferred adsorber is molecular sieve coke which preferentially adsorbs the oxygen. The process permits air to be enriched to such an extent that the product fraction, namely, the second fraction, removed from the adsorber contains between 70 and 95 volume percent of oxygen.