Unicracking-JHC is a modern regenerative fixed-bed catalytic process for selectively converting high boiling hydrocarbons such as virgin, steam cracked and coker gas oils and catalytic cycle oils to lower boiling products-gasoline, jet fuel and diesel oils-with a net consumption of hydrogen. Various conversion levels are possible including total conversion to gasoline and lighter. With complete conversion, liquid yield of 120-130 volume percent of feed are common.
Unicracking-JHC process utilizes a high activity catalyst which has excellent activity maintenance in the presence of nitrogen and sulfur compounds. Typical reaction temperatures are 500-800°F and operating pressures range from 800-2, 000 psi, exact conditions being fixed by feed stock propeties and processing objectives. Either singlestage or two-stage hydrocraking may be employed. The choice depends on feed rate, feedproperties, processing objectives. For most stocks, recent technological develop-ments permit economic conversion to gasoline and lighter products in a single stage.
Eight Unicracking-JHC units totaling 90, 000 BPSD of capacity are now on stream, and other units under construction or announced will bring the total to about 200, 000 BPSD by the end of 1968.

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The shift reaction of carbon monoxide is mainly used to produce the hydrogen and to detoxify the town gas.
The auther listed up the date of equilibrium constants, heats of reaction and free energies. Rate equations and reaction mechanisms are described.
The CO conversion catalysts are eluciadated in next section. There are two types of conversion catalysts which are employed industrially today; one is the iron-chromium oxide catalyst (high temperature catalysts), and the other is copper (-chromium)-zinc oxide catalysts (low temperature catalyst). The copper (-chromium)-zinc oxide catalyst is very active at low temperature, but this catalyst is expensive and sensible to sulfur compounds. Recently, it was found that the cobalt molybdenum sulfide catalyst was active for this reaction at 300-400°C. This catalyst is tested on pilot plant scale today.
In the last section, the outlines of CO converter and process diagrams are written.

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Many studies concerning the oxygen containing functional group in coal substance and its extracts have been done to investigate its chemical properties and structure. On the other hand, little has been known of the behaviours of functional oxygen groups in coal by heat-treatment. Present authors determined the contents of carboxyl, hydroxyl and carbonyl groups in twelve Japanese coals, five foreign coals and the heat-treatment products of these coals, and attempted to clarify the behaviours of oxygen containing functinal groups in the early state of carbonization (200-500°C).
As for the analytical methods of carboxyl, hydroxyl and carbonyl groups, ion exchange method in aqueous calcium acetate solution, acetylation method in acetic anhydride-pyridin solution and oximation method with hydroxyl amine hydrochloric acid in pyridine were adpoted respectively.
The results of determination of carboxyl and hydroxyl groups in original coals agreed with those reported by Blom etal., Friedman etal., Halleux etal., Takeya etal., and so on. As for carbonyl groups in original coals, relatively good agreements were obtained when comparing our results with those reported by Halleux etal. and Takeya etal., but there were large differences between our results and those reported by Blom etal. especially in the range from 70%°C to 80%°C.
The carboxyl, hydroxyl and carbonyl groups in original coal decreased almost lineally with coal rank.
The behaviours of functional oxygen groups by heat treatment were characteristic of the coal rank of original coals. In low rank coals, the functional oxygen groups decreased gradually above a certain heat treatment temperature (HTT), and the higher the coal rank, the higher the temperature where the functional groups began to decrease.
In caking or coking coal, however, the functional oxygen groups began to increase at about 350°C and had a maximum at about 400°C.
The rest oxygen of all coals investigated, with the exception of that of Tempoku coal (the lowest rank coal), decreased slightly at first and then abruptly with HTT and had a minimum at about 400°C and again increased abruptly at 450-500°C. The rest oxygen of Tempoku coal began to increase at about 250°C and continued to increase with HTT.
These tendencies agreed qualitatively with those reported by Angelova etal.
Considering the yields of heat treated coals, discussion about the oxygen balance by heat treatment was also made.

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In order to find suitable combutsion catalyts for the complete combutsion of automobile exhaust gases many metal oxide mixture catalysts have been studied. Activities of the catalysts have been examined on the oxidation of methane and carbon mono-oxide, and thermostabilities of the catalysts have been tested on the activities after thermal treating.
Two component iron oxide catalysts, Fe₂O₃-Mn₂O₃, Fe₂O₃-Cr₂O₃ Fe₂O₃-CO₃O₄, and Fe₂O₃-CuO are very active, but their stabilities at high temperature are very low. Among the three component iron oxide catalysts, Fe₂O₃-Mn₂O₃-Al₂O₃ (50: ₂5: ₂5 wt%) and Fe₂O₃-CuO-Al₂O₃ (50: ₂5: ₂5 wt%) have acceptable activities and thermal stabilities.
CuO-Al₂O₃ is the most active and thermostable catalyst among the co-precipitated CuO, Mn₂O₃ and, or Cr₂O₃-Al₂O₃ catalysts. CuO-Al₂O₃ changes into cupric aluminate at high temperature, but this aluminate has high catalytic activity, thermostability of CuO-Al₂0₃ catalyst is caused by this property.
CuO-MgO-Al₂O₃ catalysts are more active and stable than CuO-Al₂O₃. It pro-motes activity for oxidation of carbon mono-oxide to add manganese oxide to CuO-MgO-Al₂O₃, and adding zinc oxide promotes activity for oxidation of methane.
Differences about poison sensitivities of several catalysts tested have not been recognized with lead bromide poisoning.

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