1494. HORNE, W. A., AND FARAGHER, W. F. Interrogation of Dr. Pier and Staff. I. G. Farbenindustrie A.-G. Ludwigshafen and Oppau. II. Synthesis of Hydrocarbons From Water Gas – Michael Process. FIAT Rept. 426, 1945, pp. 1-8. PB 1367 and 7745; TOM Reel 199; Bureau of Mines Inf. Circ. 7376, 1946, 27 pp.; Coke Smokeless-Fuel Age, 1946, pp. 194-195.

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Literature Abstracts

Four processes developed to the pilot plant scale by the I. G. Farbenindustrie A.-G. at Ludwigshafen under the direction of Dr. Michael are described. The fixed-bed circulating-gas process uses a fixed catalyst made by pasting powdered Fe carbonyl with a concentrated borax solution equivalent to about 1% on the Fe and sintering 1 c. of the paste at 800°-850° for 4 hr. and cooling in an H₂ atmosphere. The synthesis gas is recirculated over this in the ratio of 100 vol. of old gas to 1 vol. of new, having a CO:H₂ ratio of 1:1 or 4:5, a S content of less than 2 mg. per m.³ and no CO₂, so that the rise in temperature in the catalyst bed is not over 10°. The gas velocity is about 1 m. per sec. and the time of contact 0.5-1 sec. The flow must be nonturbulent. Operating pressure is 20 atm. and the temperature 300°-325°. The yield of hydrocarbons per m.³ of catalyst is 700-800 kgm. per day recovered in 3 stages of condensation. 1 m.³ of 4 CO:5 H₂ gas yields about 35 gm. of CH₄ and C₂H₆ and 160 gm. of useful products; the gasoline having an octane number of 68-70 and the gas oil a cetene number of 45-50. In the oil-circulation process an oil fraction from the synthesis product is circulated over the catalyst to remove the heat of reaction and prevent excessive production of C and CH₄. The process operates at 20-25 atm. pressure and temperatures of 260°-300° in the first stage and 280°-330° in the second. It uses the same catalyst as the first process. The gas has a CO:H₂ ratio of 55:45 and the yield per liter of catalyst per hr. is 20-25 gm. of all products and per m.³ of synthesis gas 150 gm., the gasoline having an octane number of 62-625 and gas oil a cetene number of 70. Foam process has for its object the production of a higher proportion of olefins in the product. It operates in the liquid phase using a finely divided catalyst suspended by an ascending stream of gas. The catalyst is made by precipitation of Fe₂O₃ and is pasted into granules with a solution of K₂CO₃, dried, reduced by H₂ at 350°-450° and ground fine in a ball mill mixed with gas oil. A gas of composition CO:H₂=1:1 or 4:5 is used at 20 atm. pressure and 250°. The time of reaction is 3 minutes. The temperature rise through the reaction chamber is about 10°. Conversion to useful products is about 70% and the CO₂ content of the exit gas is 40-45%. The yield per day per m.³ of reaction products is 350-450 kg. The gasoline has a 70% olefin content and the gas oil 40-50%. In tubular reactor process, the operating pressure is 20 atm. and the temperature 230°-250°. The synthesis gas has a CO:H₂ ratio 4:5 to 5:5. The catalyst is made by mixing Fe₂O₃ with 5-25% of alkali earth and 1-2% of K₂CO₃, pelleting, heating to 850°, cooling to 350°-450° and reducing in H₂. It has a high activity at 240° and below. Conversion is 70-80%, giving 0.35-0.45 kg. per liter per day of products all of high olefin content.