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轻油
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  light oil
    Comparison of Two Steam Reforming Catalysts for Light Oil
    两种轻油水蒸汽转化催化剂的比较
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    An experimental study on Type CN-14 catalyst for pre-reforming of light oil to CH_4- rich gas
    CN-14型轻油预转化制富甲烷气催化剂的实验室研究
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    Application of Technology for Gasmaking with Light Oil for Town Fuel Gas
    轻油制气技术在城市燃气中的应用
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    Study on improving the yield of RFCCU light oil using acid additives
    用酸性助剂提高RFCCU轻油收率
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    Application of RS3 in Gasmaking with Light Oil
    RS3在轻油制气中的应用
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  “轻油”译为未确定词的双语例句
    PERFORMANCE AND APPLICATION OF NAPHTHA STEAM REFORMING CATALYSTS, Z402/Z405 AND Z409/Z405G,FOR HYDROGEN PRODUCTION
    Z402/Z405 Z409/Z405G轻油蒸汽转化制氢催化剂性能及其应用
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    Operational Performance of Z402 Commercial Steam Reforming Catalyst for Naphtha
    工业条件下Z402轻油蒸汽转化催化剂性能研究
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    Comprehensive Evaluation of the Performances of Naphtha Steam Reforming Catalysts Z402/Z405G after Commercially Used
    轻油蒸汽转化催化剂Z402/Z405G工业应用后性能综合评价
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    STUDY ON PRODUCTION OF EXTRACTIVE SOLVENT OIL NO 6 BY USING THE AROMATICS RAFFINATE OF THE SPLITTING LIGHT-END PRODUCTS
    轻油裂解芳烃抽余油生产6号抽提溶剂油的研究
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    DEVELOPMENT OF 3955 HYDROCRACKING CATALYST
    3955轻油型加氢裂化催化剂的研制
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  light oil
Flow-injection photometric determination of mercaptans in light oil products with chromatomembrane extraction
      
A procedure was developed for the flow-injection photometric determination of mercaptans in light oil products.
      
Modeling of Liquid-Vapor Equilibrium in Systems Including a Light Oil-Gas Component and Aromatic and Polyaromatic Hydrocarbons
      
During this process, the oil is partially transformed into hydrocarbons, light oil, semiliquid and solid bitumens.
      
The micropacked columns were successfully applied to the separation of components of a light oil and a kerosine.
      
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From the experimental results,the phase diagrams,which correlate the temperature,pressure and percentage of vaporization of equilibrium flash vapori- zation of shale oil,are constructed.The focal point on the phase diagram of No.1 light gas oil of Fushun shale oil is 39.3 atm.(F_p)and 482℃(F_t);and that of Fushun crude shale oil is 30.1 atm.(F_p) and 558℃(F_t). The values of the focal points calculated by the empirical graph of Edmister show certain deviations from the experimental results,and these deviations...

From the experimental results,the phase diagrams,which correlate the temperature,pressure and percentage of vaporization of equilibrium flash vapori- zation of shale oil,are constructed.The focal point on the phase diagram of No.1 light gas oil of Fushun shale oil is 39.3 atm.(F_p)and 482℃(F_t);and that of Fushun crude shale oil is 30.1 atm.(F_p) and 558℃(F_t). The values of the focal points calculated by the empirical graph of Edmister show certain deviations from the experimental results,and these deviations will be larger if the empirical graph of Okamoto is used.But the theoretical methods of calculation developed by Katz and Brown or Edmister give much better results as compared with above empirical methods.Therefore,the theoretical method can be applied to calculate the data of equilibrium flash vaporization of shale oil and shale oil fractions.

从实验得到了推算页岩油平衡汽化的温度-压力-汽化率的关系相图.抚顺页岩油一号轻油相图焦点为:F_p=39.3大气压,F_t=482°;抚顺页岩原油相图焦点为:F_p=30.1大气压,F_t=558°.应用 Edmister 的石油经验图所推算的平衡汽化率或相图焦点,与实验值是有一定偏差的.而用 Okamoto 的经验图推算的平衡汽化率则偏差更大。若以实沸点代表组成,应用实验的蒸汽压换算表求得平衡常数,然后进行抚顺页岩油一号轻油和抚顺页岩原油的平衡汽化率理论计算,则得到与实验值一致的结果;并且远较 Okamoto 或 Edmister 的经验方法好.因此,直接用理论方法来计算页岩油馏分或页岩原油的平衡汽化性质可以得到满意的结果.

The solubility equilibria between No.1 light gas oil and liquid SO_2 as well as the distribution of the sulfurous,nitrogenous,and some unsaturated com- pounds(94% H_2SO_4 soluble)in above two phases at -10°,0° & 20℃ were presented. In comparison with other solvents,liquid SO_2 is an excellent solvent for refining shale oil,as it has better selectivity and higher capacity for extrac- tion of sulfur and nitrogen compounds.It was found that at 0℃,with liquid SO_2/oil ratio 0.65(volume ratio)and two theoretical...

The solubility equilibria between No.1 light gas oil and liquid SO_2 as well as the distribution of the sulfurous,nitrogenous,and some unsaturated com- pounds(94% H_2SO_4 soluble)in above two phases at -10°,0° & 20℃ were presented. In comparison with other solvents,liquid SO_2 is an excellent solvent for refining shale oil,as it has better selectivity and higher capacity for extrac- tion of sulfur and nitrogen compounds.It was found that at 0℃,with liquid SO_2/oil ratio 0.65(volume ratio)and two theoretical stages,the refined pro- ducts satisfy the requirements for the kerosene and light diesel oil. A method for the solubility equilibrium prediction and an empirical for- mula for calculation of the refined product yield were also given.

测定了液体二氧化硫和抚顺页岩1号粗轻油在-10°、0°和20°时的液-液平衡溶解度,以及硫、氮和不饱和分在上述两相中的分布情况.试验证明,液体二氧化硫是一种精制页岩油的优良溶剂.与其他溶剂精制法比较,其选择性、脱硫和脱氮效率均较高;在得到相同氮含量和硫含量的产品时,所需的溶剂量及处理段数均最少.确定用二氧化硫精制的适宜条件为:温度0°,溶剂用量比为0.65(体积),处理段数为两段.在上述条件下经过处理后,所得精制油基本上可以合乎煤油和高速柴油的规格.根据实验结果提出了平衡数据的推算方法,并求得计算在不同条件下精制油收率的经验公式.

Investigations of hydrogenation of No. 1 light gas oil and absorbed oil from Fushun oil shale at 70 and 200 atm. with catalyst MoS_2-active carbon were made. The hydrogenate above 220℃ from hydrogenation of No. 1 light gas oil at 70 atm. can be used as No. 10 diesel oil, and the fraction below 220℃, if mixed with the absorbed oil and hydrogenated at 70 atm. once more, can produce jet fuel T-2. It was found that the 50% boiling point range 150—182℃ of the hydrogenate may be considered as the main constituent...

Investigations of hydrogenation of No. 1 light gas oil and absorbed oil from Fushun oil shale at 70 and 200 atm. with catalyst MoS_2-active carbon were made. The hydrogenate above 220℃ from hydrogenation of No. 1 light gas oil at 70 atm. can be used as No. 10 diesel oil, and the fraction below 220℃, if mixed with the absorbed oil and hydrogenated at 70 atm. once more, can produce jet fuel T-2. It was found that the 50% boiling point range 150—182℃ of the hydrogenate may be considered as the main constituent of jet fuel. In one stage hydrogenation of No. 1 light gas oil at 200 atm. with MoS_2 catalyst, the yield of jet fuel T-2 is 24.7%. If submitted the diesel oil fraction to further destructive hydrogenation, 12.9% jet fuel and 22.9% base oil of aviation gasoline were obtained.

進行了在MoS_2-活性炭催化劑上撫順頁岩一號輕油及頁岩回收輕質油的中壓和高壓加氫試製航空煤油的研究.一號輕油在70大氣壓下加氫所得的高於220°的餾分可作為10號柴油用;低於220°的餾分與回收輕質油混合再在70大氣壓下加氫一次,則可以得到T-2航空煤油.我們發現50%的沸點範圍為150—182°的加氫生成油可以作為航空煤油的主要組分。在MoS_2催化劑上,一號輕油經200大氣壓一段加氫,可得到T-2航空煤油24.7%;一段加氫所得柴油餾分再進行一次裂解加氫,可得到12.9%的航空煤油和22.9%的航空基油.

 
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