The study was made on the effect of faults of partially separating flow field between injection and producing wells on sweep efficiency of water flooding recovery with the aid of a potentiometric model. The sweep efficiency depends on the length, position, orientation of the faulting system with respect to the direction of the flood, and ratio of the permeability of the fault to that of the medium.
It was found that the sweep efficiency may be reduced to one half or less when the impermeable faults, whose lengths exceed 7/8 of the well spacing, extend perpendicular to the direction of the flood. For constant fault length, for faulting perpendicular to the flooding direction, the sweep efficiency is a minimum at b=0.3d, where b is the distance between faults and injection well, and d is the spacing from the injection well to the producing well. Where faults are at angles to the direction of flood, the sweep efficiency is a minimum at θ=(1/3)π, where θ is the angle between the fault and the flood direction.
The sweep efficiency for a semi-permeable faulting system is larger than that for an impermeable faulting system at a constant fault length, and less than that for a non-faulted system. The longer the fault, the greater would be the effect of permeability ratio on sweep efficiency.
Where injection and producing wells must be partly separated by faults, a greater sweep efficiency will be obtained when the injection well is located such that the area between the injection well and the fault is greater than the area between the producing well and the fault.

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Hydrodesulfurization of petroleum distillates was studied kinetically to obtain the relationship between the process variables and the desulfurization degree. The oils used as the feed were straight heavy naphtha and gas oil obtained from an Arabian crude, the total sulfur content of which was 2.5%. With both of the naphtha and the gas oil, the ratio of total sulfur content of the feed to that of the product σ°/σ^f, could be expressed by the formula
k=RT/gM_Lρ(1+m)[LHSV]ln(σ°/σ^f)
which was in good agreement with the experimental results, where m is the hydrogen to oil mole ratio, M_L is the average molecular weight of oil, ρ is the density of oil, T is the absolute temperature and k, g, R are constants.

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Heavy oil was cracked in the presence of catalyst to produce oil gas. After examining variety of catalysts, it was found that basic catalysts and nickel catalysts, especially nickel dolomite catalyst were suitable for this purpose. V₂O₅ showed best result as promoter when 0.5%∼1.5% by weight was added to nickel-refractory catalysts. Although nickel catalyst is deactivated by deposits of carbon or sulphur compounds, its activity is restored by blasting operation. Prolong use of catalyst under coke deposit will render its reactivation difficult. From the investigation on the heat-resistance properties of nickel catalysts, it was found that alumina and dolomite were good carriers, but the activity of nickel-alumina catalyst were inferior to that of nickel-dolomite catalysts. By use of nickel-dolomite catalyst the optimum conditions were decided. This catalyst has withstood thousand hours of use.

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In technical analysis of gases and liquids a mass spectrometer has been used chiefly as a quantitative analysis apparatus and there have been few attempts to apply the spectrometer to qualitative analysis. The reason is that qualitative analysis of mixtures by the use of a mass spectrometer does not work well. Due to the recent development of a gas chromatograph, however, we are now able to separate many compounds into their individual components. Our idea is to combine the use of a gas chromatograph with that of a mass spectrometer: we first separated sample compounds into their components by the use of the former and then we attempted to make a qualitative analysis of these components by the use of the mass spectra of the latter. As for the above qualitative analysis by the use of mass spectra, we used the method of identifying each hydrocarbon through the pattern coefficients of mass spectra.
We divided mass spectra into several groups and determined a base peak in each group. Next we calculated the ratio of each peak to the base peak and then changed the obtained ratio into its logarithm. Then we plotted logarithms against mass numbers (M/e) and thus we succeeded in identifying the type of each hydrocarbon.

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A dimethylformamide column (4m.) with activated alumina as the solid support in place of inactive support is capable of effecting complete gas chromatographic analysis of all 13 components usually present in gaseous hydrocarbons (C₁ to C₄) at room temperature in a short period within 30 minutes. In this adsorption-partition column, the activated alumina for the solid support is calcined (2 hours at 700C) to completely remove water of crystallization and change it to γ-alumina. By the use of γ-alumina as a support, separation of 1-butene and isobutene, and of propylene and isobutane, which are difficult to separate by the usual partition column, has been considerably improved. The stationary liquid of low boiling point, dimethylformamide, is strongly adsorbed on the solid support and life of the column, even when used at room temperature, is quite long. By addition of a small quantity of squalane to dimethylformamide, it becomes possible to completely analyze 15 components, including isopentane and n-pentane, under the same conditions. This kind of adsorption-partition column shortens the time required for complete analysis of gaseous hydrocarbons from 1/3 to 1/5 of the dimethylsulfolane column now being widely used.

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The increase of compression ratio of autmobiles has caused the octane problems of gasolines to become a very important problem in Japan as well as in other countries. This paper tries to present the data regarding octane problems in Japan, such as octane number requirements of Japanese automobiles, the road octane number characteristics of commercial gasolines and the relation between road and laboratory octane numbers.

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Study was made on the formation of sulfide film on iron surface by using radioactive sulfur and disulfides, and discussions on the composition of sulfide film and the differences in the behavior of sulfur and disulfides with the changes in atmosphere in the course of the formation of sulflde film are given.

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The authors studied factors influencing the dielectric behaviors of insulating oil by investigating its hydrocarbon composition and trace of impurities picked up during the process of refining.
The raw transformer oil distillate was separated into varied group of hydrocarbon by means of chromatographic adsorption and their electrical properties examined.
It was found that the polycyclic aromatics imparted the most unfavorable properties and resins also had a deleterious effect on the electrical properties of the oil.
On the authors' assumption that the trace of impurities could be metallic soap, numerous metallic soaps prepared in the authors' labortory were added to the refined oil in minute quantities and its effect on the electrical properties of the oil studied.
The result of the study revealed that metallic soap not only degraded the electrical properties but caused poor stability of the oil against oxidation.
From these observations, some suggestions for improving the properties of insulating oil are given.

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Three types of residue from Arabian crude were blown in a 150l capacity pilot vertical converter and no scale effect was found for the same stock when the distilled oil was totally refluxed. In this investigation the blowing conditions did not affect the relations of penetration, softening point and ductility for the same stock.
The penetration of asphalt under process of blowing can be predicted easily from the softening point determined by the rapid method proposed by the authors, i. e. the application of P. I. diagram prepared from the same stock. The penetration can also be predicted from the total oxygen consumption.
Direct injection of water into asphalt during the blowing process is effective mean of controlling its reaction temperature and its cooling efficiency has been found to be high.

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In this report, relation between increase of volume of carbon tetrachloride solution saturated with ethylene and pressure was determined at 20°C and 30°C in a view of industrial application. Telomerization was carried out at comparatively high "volume ratio". Effect of increase of carbon tetrachloride volume on the relative concentration of ethylene, reaction pressure, composition of α, α, α, ω-tetrachloroalkane, was studied. Azo-bis-iso-butyronitrile was used as initiator and benzoyl peroxide and di-tert-butylperoxide were also used for comparison⁸⁾.

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(1) By reacting propylene with ammonia, using cobalt or nickel catalyst, with no regard to the kinds of carrier or promotors, acetonitrile, propionitrile, i- and n-butyronitrile were obtained.
Particularly, with nickel catalyst, i- and n-butyronitrile were obtained principally. With cobalt catalyst, by using suitable promoter and under suitable conditions, propionitrile was obtained to a certain degree.
With molybdenum or wolfram sulfide-alumina, acetonitrile was predominantly obtained accompanied by a small amount of propionitrile.
With Ni-MgO-K. G., the reaction factors were investigated.
(2) By reacting ethylene with ammonia in the existence of nickel catalyst, propionitrile was predominantly obtained along with small amounts of acetonitrile.
With Ni-MgO-K. G., the reaction factors were studied.
(3) By reacting butylene-1 and -2 mixtures with ammonia in the existence of nickel or cobalt catalysts, acetonitrile, propionitrile, n-butyronitrile, sec.- and n-valeronitrile were obtained. And also with i-butylene, acetonitrile, propionitrile, i-butyronitrile, i- and n-valeronitrile were obtained. With nickel catalysts, valeronitrile was obtained predominantly.
(4) The order of the reactivity of alkenes to ammonia is ethylene>propylene>butylene, considering from the conversion rate of alkenes to the total nitriles.

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The rates of hydrogenolytic dealkylation of xylene isomers and ethylbenzene have been investigated, with a bench scale high pressure flow reactor under high pressures ranging from 10 to 40atm, at reaction temperatures from 590 to 680°C, contact time from 10 to 60sec. and molar ratios of hydrogen to hydrocarbons form 3 to 11.
The study has disclosed the fact that the hydrogenolytic demethylation rates of xylene isomers to produce toluene can be expressed approximately by 1.5 order equation, as is the case with that of toluene to benzene, that is, 1.0 and 0.5 order with respect to partial pressure of xylene isomer and that of hydrogen, respectively. The followings are the ratios k₁/k₂, where k₁ means the rate constant for a xylene isomer, and k₂ for toluene which had been determined already in our preceding experiment.
k₁/k₂
Temperature o-Xylene m-Xylene p-Xylene
@590°C 3.0 2.0 2.4
@680°C 3.0 2.1 2.2
The analysis of dealkylation products of ethylbenzene has suggested that the reaction is fairly complicated one, consisting of deethylation and consecutive demethylations of the alkyl chain and simultaneously of deethinylation of styrene which is formed by dehydrogenation of ethylbenzene.

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The reaction of acetic acid synthesis from methanol and carbon monoxide has been investigated kinetically in the presence of BF₃+4H₂O as catalyst at about 335° and 800atm., varying operation variables such as temperature, pressure, and charge of methanol and catalyst.
It has been found that almost all BF₃ and water consist a liquid phase into which free methanol and dimethyl ether, in dehydration equilibrium, are dissolved, and there the reaction proceeds between methanol and dissolved carbon monoxide.
A rate equation has been derived theoretically, which can explain the effects of the above-mentioned variables quantitatively; the fractional conversion rate is proportional to the fugacity of CO and to the reciprocal square root of the charged amount of methanol, and is expressed by a quadratic function of catalyst charge fraction.
The apparent activation heat is 34.1kcal/mole, and of liquid phase reaction 22.7, and the rate constant is 2.37×10^-5atm.^-1min.^-1 at 335°.

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