石油学会誌
Print ISSN : 0582-4664
4 巻, 1 号
選択された号の論文の4件中1~4を表示しています
  • 大島 昌三, 勝又 章
    1961 年 4 巻 1 号 p. 24-28
    発行日: 1961/01/25
    公開日: 2009/01/30
    ジャーナル フリー
    Rearrangement ions of hydrocarbons were investigated to make a contribution to the qualitative analysis by mass spectra. It was proved that this analysis made an impatent contribution to the qualitative analysis. The hydrocarbons used for the analysis were paraffins, naphthenes, olefins, and aromatics of C6 and lower. As these iso-paraffins, naphthenes, and olefins have many rearrangement ions, their measurements are contributed to qualitative analysis. While, n-paraffins and aromatics have rather less ions.
    Good results were obtained in the examination by ratio of mass-spectra analysis, pattern-exponent analysis and ionization method of low energy, and application of these analyses to the qualitative analysis of the unknown fraction of cracking gas separated by gas chromatography.
    The above experiment was conducted simultaneously with the measurement of rearrangement ions.
    It is believed that these results obtained by the measurement explain the study on the mechanism of dissociation of molecules through electron bombardment. Hereafter, similar measurements will be made on hydrocarbons of C7 and higher, and the mechanism of dissociation of molecules will be investigated through electron bombardment.
  • 触媒の再生および最適粒径分布について
    山口 隆章
    1961 年 4 巻 1 号 p. 29-33
    発行日: 1961/01/25
    公開日: 2009/01/30
    ジャーナル フリー
    The recent studies on the catalyst regeneration and the optimum distribution of the catalyst are reported in this paper.
    One of the difficult operations experienced in the catalyst regeneration is the secondary combustion of carbon monoxide in the regenerator. This reaction, or after-burning as it is generally referred to, is extremely exothermic and the resultant temperature rise is so great in an instant that the regenerator interior is remarkably damaged.
    The methods of preventing this after-burning are discussed as follows:
    (1) It is recommended to keep the CO2/CO ratio as low as possible. For example, reduction of CO2/CO ratio from 1.3 down to 1.2, or reduction by only 0.1, resulted in temperature drop of regenerator by 22°C (or 40°F), in which a considerably safe operation should be expected.
    (2) By tracing the location of after-burning, it was found around the outlet of the primary cyclone toward the secondary cyclone, or around the cyclone installed just above the overflow well of regenerated catalyst of low carbon content and the cyclone near by the regenerator shell. Therefore, it is essential, to improve the distribution of combustion air throuth the regenerator grid so as to reduce the locally higher oxygen content.
    The optimum distribution of particle-size shall not be precisely determimined neither by the experiences of plant operation nor by laboratory scale experiments. However, it was found that the optimum distribution decided from the standpoint of fluidization was identical with that decided from the standpoint of the catalyst regenration, and most satisfactory results were obtained in the catalyst of the following particle-size distribution:
    0-40 microns 5-10wt%
    Above 80 microns 10-20wt%
  • 高アルミナ触媒と低アルミナ触媒の比較ならびに触媒の損失について
    山口 隆章
    1961 年 4 巻 1 号 p. 34-38
    発行日: 1961/01/25
    公開日: 2009/01/30
    ジャーナル フリー
    The object of this study is a comparison of several properties between high and low alumina catalysts obtained by the operating process during which 13% alumina catalyst in the reactor-regenerator system had gradually been replaced by 25% alumina catalyst.
    Also, the catalyst loss from the regenerator stack, which has not been subjected to quantitative analysis so far, is investigated, taking the opportunity of the above-mentioned catalyst switchover.
    1. The results of comparing between high and low alumina catalysts are as follows:
    a) As for metal-resistant power of the catalyst, high alumina catalyst has shown superior results and the quantity of hydrogen production remained was about 70% of that expected in the case of low alumina catalyst under the same metal content.
    b) The catalyst loss dropped by 30-60%, which can be attributed to higher anti-erosion and smaller heat break of high alumina catalysts.
    c) High alumina catalyst exhibits an excellent retention of activity as well metal-resistance. When high alumina catalyst was used, the catalyst make-up requirement is only 70-80% (by wt.) of that of low alumina catalyst in order to keep the regenerated catalyst at the same activity level.
    d) No appreciable effects of high alumina catalyst with regard to product yields and qualities have been noticed.
    2. Quantitative measurements has not been carried out on the selective loss of the added fresh catalysts, although it has been known to some extent.
    The catalyst fines have been collected from the regenerator stack gas, and tested for particle-size distribution, activity, metal content, alumina content, etc. The results of the test indicate that a considerable amount of fresh catalyst added to the system was being lost from the stack. The loss of fresh catalyst during the time of catalyst addition amounts to 1.5 to 2.0 times as much as that in the normal operation.
    3. When the catalysts to be used are selected, due attention must be paid to its resistance to erosion and heat break as well as particle-size distribution so as to minimize the overall catalyst losses.
  • 桐生 知男, 古明地 義久, 尾上 憲司, 渡辺 喬
    1961 年 4 巻 1 号 p. 39-43
    発行日: 1961/01/25
    公開日: 2009/01/30
    ジャーナル フリー
    The airing of propylene was carried out with copper-silica gel as a catalyst in the excess of air. Assuming that the rate-determining steps were the following surface reactions,
    C3H6→C3H4O→CO
    C3H6→HCHO→CO
    C3H6→CO2
    the production of acrolein, especially the yield of acrolein by one pass flow process, was dynamically analyzed as the psuedo-primary reaction and the optimum condition of producing the maximum yield of acrolein was determined.
    The calculated apparent
    activation energies of the following processes, C3H6→C3H4O
    C3H6→HCHO
    C3H6→CO2 C3H4O→CO
    HCHO→CO
    were 15.6, 15.5, 11.9, 2.3 and 10.0kcal/mol, respectively.
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