Patent then subjected to a catalytic dehydrogenative yielding 3-methylpyridine in a second step.
Manufacture and oxygen
T. Tomita; Y. Ishiuchi; M. Kawakami et al. Mitsubishi Gas Chemical Co. Eur. Pat. Appl. 621,235, Oct. 26, 1994; Jpn.
The process involves reacting 0 with H in a reaction medium containing a Sn-modified Pt-group metal catalyst supported on a carrier (preferably a crystalline zeolite). This process does not require the presence of halogen ions and acid in the reaction medium, and the H,O, is produced at high concentrations.
Conversion of Fischer-Tropsch heavy end products with platinum/boron-zeolite f3 catalyst having a low (Y value W.S. Borghard; Mobil Oil Corp. U.S. 5,362,378,
S.S. Shih; P.J. Angevine Mobil Oil Corp. U.S. 5,362,376, Nov. 8, 1994;
of high viscosity
M.R. Apelian; CL. Baker Jr.; T.F. Degnan Mobil Oil Corp. U.S. 5,358,628, Oct. 25, 1994; Appl. July
lubricants et al. 5, 1990
Petroleum wax feeds are converted to high viscosity index Iubricants by a two-step hydrocracking-hydroisomerization process in which the wax feed is initially subjected to hydrocracking under mild conditions. The hydrocracked effluent is then subjected to hydroisomerization in a second step using a low acidity dicarboxylic acid-treated zeolite 6 or mordenite catalyst that effects a preferential isomerization on the paraffin components to less waxy, high V.I. isoparaffins.
H. Kanesaka; N. Kachi Nissan Motor Jpn. Kokai Tokkyo Koho Appls. Mar. 11, 1993
The catalysts comprise a monolithic honeycomb support loaded with a first coating layer mainly containing Ce oxide and activated alumina (free from noble metals), and a second coating layer mainly containing metal ion-exchanged zeolite powders. Preferably, Cu- or Co-exchanged zeolites are used. The catalysts show high activity in the lean burn combustion region at relatively low temperature.
of denitration them
Y. Asano; K. Kitakizaki Meidensha Electric Manufacturing Co. Ltd. Jpn. Kokai Tokkyo Koho 94,269,673; 94,269,674, Sept. 27, 1994; Appls. Mar. 18, 1993 The denitration agents are manufactured by contacting zeolites (e.g., Na-containing mordenite type) with catalytic metalcontaining solutions (e.g., Co-containing solutions) and then firing the zeolites. The denitration process comprises contacting NO,containing gases with the denitration agents in the presence of heavy oil A. The agents show long lasting catalytic activity in the reduction of NO, in diesel engine exhaust gases.
Low sulfur gasoline of relatively high octane number is produced from a catalytically cracked, sulfur-containing naphtha by hydrodesulfurization followed in a second step by treatment over an acidic catalyst system comprising an intermediate pore size zeolite having crystallites of an effective radius of at least 0.25 urn. The treatment over the large crystal acidic catalyst in the second step restores the octane loss that takes place as a result of the hydrogenation treatment and results in a low sulfur gasoline product with an octane number comparable to that of the feed naphtha. The large crystal size improves gasoline yield by reducing conversion of branched paraffins.
M. Misonoo Tokyo Gas Co. Ltd. Jpn. Kokai Tokkyo Koho 94.254,352, Sept. 13, 1994; Appl. Mar. 4. 1993 The title catalysts comprise Pd supported on an H ZSM-5 zeolite, obtained by ion exchange of NaZSM-5 zeolites with NH,’ to form NH,ZSM-5 zeolites, firing the NH,ZSM-5 zeolites into HZSM-5 zeolites, and ion exchange of the HZSM-5 zeolites in aqueous solutions containing Pd(NO,), or [Pd(NH,),lCI,. Lean burn exhaust gases containing large amounts of 0,, little amounts of lower hydrocarbons, and NO, are treated by contacting the gases with the Pd/HZSM-5 zeolite catalysts in the presence of lower hydrocarbons, if necessary, to show total hydrocarbon content enough for reduction of NO, in the treated gases. The catalysts are durable and increase denitration efficiency.
Manufacture gases with
The use of high silica to alumina ratio large pore zeolites in combination with a hydrogenation/dehydrogenation component is described, to convert Fischer-Tropsch heavy end products which may contain paraffins, olefins, and oxygenates into low pour point distillates with high cetane number and extra high V.I. lube content. The lube can be dewaxed by a conventional solvent process, by a catalytic process, or by increasing the severity of the hydroisomerization step.
Gasoline upgrading process diate pore size zeolites
Catalysts for automotive their preparation
T. Kondo; S. Asaoka; Y. Okada et al. Chiyoda Chemical Engineering Construction Co. Jpn. Kokai Tokkyo Koho 94,271,510, Sept. 27, 1994; Appl. Mar. 18, 1993 Carbonic acid esters are prepared by reaction of alcohols with CO and 0 in the presence of ion-exchanged Cu-containing zeolite catalysts (e.g., Cu-containing MFI-type zeolite [Cu/AI atomic ratio = 0.491).
Preparation of alkyl tertiary alkyl ethers from primary and tertiary alcohols using platinum/palladiummodified f3-zeolite catalysts J.F. Knifton; P.S.E. Dai Texaco Chemical Co. U.S. 5.364.981, Nov. 15, 1994; Appl. Nov. 8, 1993 Alkyl tertiary alkyl ethers were prepared by continuously contacting a C,-, primary alcohol with a C,,, tertiary alcohol (IO: l-1:10 molar ratio) at 20-250°C and 15-1,000 p.s.i. in the presence of a 8-zeolite catalyst, modified with 2 1 group VIII metals and optionally modified further with a halogen or a group IB metal. The catalyst was reduced in a stream of H at IOO-600°C.
N. Ito; T. Yokoi; T. Yoshida Toa Gosei Chemical Industries Jpn. Kokai Tokkyo Koho 94,256,250, Sept. 13, 1994; Appl. Mar. 8, 1993 Heating R’R*CHCX, or R’R’C:CX, [R’, R* = H, halo, (halogenated) C,-, alkyl, (halogenated) Cs-,o aryl, (halogenated) C,-,, alicyclic hydrocarbyl; R’ and R2 are not trihalomethyl or do not contain a trihalomethyl group; X = halo] in the presence of an acid-type zeolite catalyst and H,O gives monocarboxylic acids R’R’CHCO 2 H.
T. Tatsumi; H. Sakashita Tosoh Corp. Jpn. Kokai Tokkyo Koho 94,256,232, 1993 Aromatization of C,, hydrocarbons of a catalyst consisting of a noble
is effected in the presence metal and an alkali metal salt