Standard Oil Company Indiana process

This process has many similarities to the Phillips process and is based on the use of a supported transition metal oxide in combination with a promoter. Reaction temperatures are of the order of 230-270°C and pressures are 40-80 atm. Molybdenum oxide is a catalyst that figures in the literature and promoters include sodium and calcium as either metals or as hydrides. The reaction is carried out in a hydrocarbon solvent. 

The products of the process have a density of about 0.96 g/cm, similar to the Phillips polymers. Another similarity between the processes is the marked effect of temperature on average molecular weight. The process is worked by the Furukawa Company of Japan and the product marketed as Staflen. 

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Chlorex (1) A process for extracting lubricating oil stocks from petroleum fractions using 0,0-dichloro diethyl ether. Chlorex is also the trademark for this compound. Developed by Standard Oil Company (Indiana) in the early 1930s and used until the 1960s. 

Mid-Century Also called M-C. A process for oxidizing p-xylene to terephthalic acid, using oxygen in acetic acid and catalyzed by a mixture of cobalt and manganese bromides. Developed in the 1950s by Halcon International and commercialized by Standard Oil Company (Indiana). The first plant was built at Jolet, IA, in 1938. The Amoco and Maruzen processes are improved versions. 

Some years ago, Standard Oil Company (Indiana) published a 70-page booklet entitled Hazards of Water in Refinery Process Equipment. [1] This booklet appears to be a bible for hands-on refinery employees, and it provides easy-to-understand fundamentals on the hazards. The booklet concludes with these thoughts ... 

Standard Oil Company (Indiana), Hazards of Water in Refinery Process Systems, Chicago, 111.,... 

A second process using complex as the catalyst was independently developed by the Standard Oil Company (Indiana) and by the Texas Company (25,26). A simplified flow diagram of this liquid-phase process is shown in Figure 17. A portion of the dried and heated feed passes through a saturator where aluminum chloride is picked up in accordance with the solubility curve shown in Figure 8. The total feed combined with re( y< le hydrogen chloride enters the bottom of the reactor and... 

Pentane isomerization was used to increase the critical supply of aviation gasoline toward the end of the war. Two processes—one developed by Shell and one by Standard Oil Company (Indiana)—were commercialized. The pentane processes differ from butane isomerization mainly in the use of somewhat milder conditions and an inhibitor to suppress side reactions. In general, the problems of the butane processes are inherent also in pentane isomerization, but the quality of the feed stock is less important. Olefins can be as high as 0.2 %, although 0.05 % is preferable. The hexane content should not exceed about 5%, and sulfur and water contents should be as low as in the butane process. Catalyst life is much shorter than in the butane processes only about 30-50 gallons of isopentane are produced per pound of aluminum chloride. 

The other commercialized pentane process is that of the Standard Oil Company (Indiana) (8,26). This process differs from the Standard (Indiana)—Texas butane process in that 0.5% benzene is added to inhibit disproportionation and the make-up aluminum chloride is added directly to the reactor as a slurry. 

The only commercial isomerization of light naphtha was carried out in two plants employing the Isomate process developed by the Standard Oil Company (Indiana). In this process (26), a feed containing normal pentane and low-octane-number hexanes is converted to isopentane and hexanes of higher octane number. Pentanes and hexanes in any ratio can be processed. By recycle of selected fractions of the product, concentrates of isopentane or of neohexane (2,2-dimethylbutane) and diisopropyl (2,3-dimethylbutane) can be made as the final products. 

In the fluid-catalyst process, finely divided catalyst powder is continuously circulated from reactor to regenerator and back again without mechanical means. The fluid process was originated by the Standard Oil Development Company, the research organization of the Standard Oil Company of New Jersey, in collaboration with The M. W. Kellogg Company and Standard Oil Company (Indiana). Other companies participating in the development were Anglo-Iranian Oil Company, Ltd., Shell Oil Company, The Texas Company, and Universal Oil Products Company. This process was first announced in 1941 (48). 

The solution to the problem came as early as 1913, when William Burton of the Standard Oil Company (Indiana) put into operation a series of thermal cracking units known as Burton Stills, This was the beginning of a method for breaking the larger carbon molecules into smaller ones through a heat process, a process for making chemicals such as ethylene, propylene, butylene, and other olefins from crude oil. 

Isoforming A process for increasing the octane rating of thermally cracked gasolines by catalytic isomerization over silica/alumina. Terminal alkenes are thus converted to nonterminal alkenes. Developed by Standard Oil Company of Indiana in the 1940s. 

Ultraforming A catalytic reforming process developed by Standard Oil of Indiana and licensed by Amoco Oil Company. The catalyst contains platinum and rhenium, contained in a swing reactor - one that can be isolated from the rest of the equipment so that the catalyst can be regenerated while the unit is operating. The first unit was commissioned in 1954. 

A semicommerdal plant based on this process was built and operated for the Manhattan I oject by the Standard Oil Company of Indiana [C4]. In 1953, the U.S. Atomic Energy Commission authorized construction of a larger plant at Niagara Falls, New York, with the Hooker Electrochemical Company as operating contractor [M3]. This plant produced 460 kg/year of B at an enrichment of 92 a/o B. The plant was shut down in January 1958. Eagle Picher Industries, Inc., has been producing 6 at Quapaw, Oklahoma, by this process since 1973 and is expanding capacity to 1000 kg/year. The cost is from 5 to 15/g. 

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