Abstract: A hydrocracking catalyst for heavy hydrocarbon oils comprising a metallic element of the VIb Group and a metallic element of the VIII Group supported on a carrier containing a novel faujasite-type aluminosilicate which absorbs an infrared in a frequency region of 3740.+-.10 cm.sup.-1 in an absorption percentage A of at least 20% and absorbs an infrared in a frequency region of 3560 .+-.10 cm.sup.-1 in an absorption percentage B of at least 5%, the ratio of A/B being at least 2, has a specific surface area of at least 650 m.sup.2 /g, has a framework SiO.sub.2 /Al.sub.2 O.sub.3 molar ratio of from 20 to 50, and has a lattice constant of from 24.15 to 24.50 .ANG.. The novel faujasite-type aluminosilicate is produced by treating a faujasite-type zeolite with an acid.

Abstract: A process for hydrocracking heavy oil which comprises hydrocracking the heavy oil in the presence of a catalyst comprising a support of 10 to 90% by weight of an iron-containing aluminosilicate and 90 to 10% by weight of an inorganic oxide, and at least one metal belonging to Group VIB of the Periodic Table and at least one metal belonging to Group VIII deposited on the support. The iron-containing aluminosilicate has a composition of the formula expressed as oxides: aFe.sub.2 O.sub.3 .multidot.Al.sub.2 O.sub.3 .multidot.bSiO.sub.2 .multidot.nH.sub.2 O wherein n is a real number of 0 to 30, and a and b are real numbers satisfying the following relationships: 15<b<100, 0.005<a/b<0.15; and has an inert iron compound content, (Fe).sub.dep, as calculated by a temperature programmed reduction, of not more than 35% of the total iron content; and when subject to a temperature programmed reduction, Th (.degree.C.), is within the following equation: 850.degree. C..ltoreq.Th.ltoreq.(-300.times.UD+8,300).

Abstract: An iron-containing aluminosilicate and a process for producing the iron-containing aluminosilicate. The iron-containing aluminosilicate has a composition of the formula expressed as oxides: aFe.sub.2 O.sub.3.Al.sub.2 O.sub.3.bSiO.sub.2.nH.sub.2 O wherein n is 0 to 30, and a and b are numbers satisfying the following relationships: 15<b<100 and 0.005<a/b<0.15. The iron-containing aluminosilicate has an inert iron compound content (Fe).sub.dep as calculated by a temperature-programmed reduction, of not more than 35%, and at least one high-temperature reduction peak, Th (.degree. C.), within the following equation: 700.degree.C..ltoreq.Th.ltoreq.(-300.times.UD+8,320).degree. C. wherein UD is a lattice constant (.ANG.) of the iron-containing aluminosilicate.

Abstract: A hydrocracking catalyst for heavy hydrocarbon oils comprising a metallic element of the VIb Group and a metallic element of the VIII Group supported on a carrier containing a novel faujasite aluminosilicate which absorbs infrared in a frequency region of 3740.+-.10 cm.sup.-1 in an absorption percentage A of at least 20% and absorbs infrared in a frequency region of 3560.+-.10 cm.sup.-1 in an absorption percentage B of at least 5%, the ratio of A/B being at least 2, has a specific surface area of at least 650 m.sup.2 /g, has a framework SiO.sub.2 /Al.sub.2 O.sub.3 molar ratio of from 20 to 50, and has a lattice constant of from 24.15 to 24.50 .ANG.. The novel faujasite aluminosilicate is produced by treating a faujasite zeolite with an acid.

Abstract: A catalyst composition for the hydrogenation of heavy hydrocarbon oil, where the catalyst composition comprises at least one active ingredient for hydrogenation supported on a porous alumina carrier and has the following characteristics: (1) the total volume of the pores therein is from 0.4 to 1.0 ml/g; (2) the mean pore diameter of pores having a pore diameter of from 5 to 400 .ANG. is from 60 to 140 .ANG.; (3) the volume of pores having a pore size within .+-.25% of the mean pore diameter of pores having a pore diameter of from 5 to 400 .ANG. is from 60 to 98% of the volume of pores having a pore diameter of from 5 to 400 .ANG.; (4) the volume of pores having a pore diameter of from 400 to 5000 .ANG. is from 2 to 9% of the total volume of the entire pores; (5) the ratio (mm.sup.2 /mm.sup.3) of the outer surface area of a molded catalyst powder to the volume thereof is from 4 to 8; and (6) all points in the interior of the molded catalyst particle are positioned within 0.05 to 0.

Abstract: A process of thermally cracking a heavy petroleum oil wherein the heavy petroleum oil is treated successively in a cracking furnace and then in a perfect mixing type tank reactor. The thermal cracking in the cracking furnace is performed at a temperature at the outlet of the cracking furnace of 450.degree.-520.degree. C. with a conversion of at least 60-75% of the overall conversion rate while the thermal cracking in the tank reactor is performed at a temperature of 400.degree.-450.degree. C. a pressure of from ambient pressure to 1 kg/cm.sup.2 for a period of time of less than 30 minutes but not less than 10 minutes while feeding steam having a temperature of 435.degree.-700.degree. C. to the tank reactor in an amount of 8-20% by weight of the heavy petroleum oil fed to the cracking furnace.

Abstract: A hydrogen treating catalyst comprising alumina, 3 to 7% by weight of nickel calculating as NiO and 10 to 20% by weight of molybdenum calculating as MoO.sub.3, which has a total pore volume of 0.55 to 1.0 ml/g, an average pore diameter of 50 to 250 .ANG., and factor P of 3 to 4, wherein the volume of pores having a diameter of larger than the average pore diameter+10 .ANG. and smaller than the average pore diameter+500 .ANG. is 10 to 30% of the total pore volume in catalyst pore distribution, wherein the factor P is represented by the following formula:P=PD/Swherein PD represents an average pore diameter measured by a mercury porosimeter which is the pore diameter (.ANG.) corresponding to the pressure at which 1/2 of the total pore volume is saturated with mercury, and S represents a proportion (%) of volume of pores in a range of PD.+-.5 .ANG..

Abstract: A method for the two-step catalytic hydrogenation treatment of a heavy hydrocarbon oil which comprisesfirst contacting the heavy hydrocarbon oil with a first solid catalyst comprising a metal component having catalytic activity for hydrogenation supported on a zeolite having catalytic activity for cracking a hydrocarbon, said zeolite having a (i) pore size distribution curve with two peaks, one peak in the range of 5 to 50 nm pore diameter and the other peak in the range of 50 to 1000 nm pore diameter and (ii) the volume of the pores having a diameter of 100 nm or larger is at least 0.05 ml/g; andthen contacting the heavy hydrocarbon oil which had been contacted with said first catalyst, with a second catalyst, said second catalyst having hydrogenation activity and which is different from said first catalyst.

Abstract: A hydrocarbon conversion crystalline catalyst composition is described comprising 5 to 90% by weight of a crystalline aluminosilicate zeolite, 5 to 90% by weight of a porous inorganic oxide, 1 to 20% by weight of a Group VI metal component (calculated as the corresponding oxide), 0 to 7% by weight of a Group VIII metal component (calculated as the corresponding oxide), and at least one of phosphorus and boron components. The weight ratio of the amount of the phosphorus+boron components (calculated as elemental phosphorus and elemental boron) to the Group VI metal component (calculated as the corresponding oxide) is from 0.01:1 to 0.08:1 and the weight ratio of each of phosphorus and boron to the Group VI metal component is below 0.045:1. This composition is prepared by contacting a support comprising the crystalline aluminosilicate zeolite and inorganic oxide with a solution containing a Group VI metal component and at least one phosphorus or boron component.

Abstract: Hydrocarbon conversion with a catalyst comprising 3 to 40 weight percent of a crystalline aluminosilicate zeolite and 60 to 97 weight percent of an alumina-magnesia matrix having a magnesia content of 2 to 50 weight percent.

Abstract: Provided is a hydrocarbon conversion catalyst comprising 3 to 40 weight percent of a crystalline aluminosilicate zeolite and 60 to 97 weight percent of an alumina-magnesia matrix having a magnesia content of 2 to 50 weight percent.

Abstract: The invention provides a process for hydrocracking heavy oils in the presence of a catalyst comprising a carrier and metals belonging to the Groups VIB and VIII of the Periodic Table. The carrier consists of from 20 to 80% by weight of iron-containing aluminosilicate and from 80 to 20% by weight of an inorganic oxide. The iron-containing aluminosilicate is prepared by treating steam-treated crystalline aluminosilicate with an aqueous iron salt solution at a pH of 1.5 or less. The molybdenum/iron-containing aluminosilicate can be used in place of the iron-containing aluminosilicate. According to the process of the present invention, the yield of an intermediate fraction can be increased.

Abstract: A process for simultaneously cracking a heavy hydrocarbons to form light oil and producing hydrogen is described, which comprises (1) a first step wherein steam and heavy hydrocarbons are simultaneously contacted with a catalyst in a reduced state, containing iron in the form of iron oxide, to produce hydrogen, cracked gases and cracked light oils, to convert the reduced-state catalyst into an oxidized-state catalyst, and to deposit coke on the catalyst, (2) a second step wherein the oxidized-state catalyst with coke deposited thereon is contacted with an oxygen-containing gas to partially combust the coke on the catalyst, to convert the oxidized-state catalyst into a reduced-state catalyst, and to fix a sulfur compound contained in the coke as iron sulfide with a part of the reduced-state catalyst; and (3) a third step wherein catalyst obtained from the second step, the major portion of the catalyst being recycled between the first step and second step, is contacted with an oxygen-containing gas at a tempera

Abstract: The invention provides a novel process for concurrently carrying out production of reduced iron and thermal cracking of heavy oils in which the reaction of thermal cracking is performed in a fluidized state with the fine iron ore as the fluidized medium and the particles of the iron ore become coated with deposits of the carbonaceous by-product material. The fine iron ore with the carbon deposited thereon is introduced in a fluidized-bed reducing furnace and there reduced into reduced iron by contacting with a reducing gas which is produced in a gas reformer from the cracked gas or the residual oil separated from the products of the thermal cracking. In an improvement of the above process, the gas reformer is operated as a fluidized-bed reactor with the reduced iron as the fluidized medium and acting as the reforming catalyst.

Abstract: A process for simultaneously cracking heavy hydrocarbons to form light oil and producing hydrogen is described, which comprises (1) a first step wherein steam and heavy hydrocarbons are simultaneously contacted with a catalyst in a reduced state, containing iron in the form of iron oxide, to produce hydrogen, cracked gases and cracked light oils, to convert the reduced-state catalyst into an oxidized-state catalyst, and to deposit coke on the catalyst, (2) a second step wherein the oxidized-state catalyst with coke deposited thereon is contacted with an oxygen-containing gas to partially combust the coke on the catalyst, to convert the oxidized-state catalyst into a reduced-state catalyst, and to fix a sulfur compound contained in the coke as iron sulfide with a part of the reduced-state catalyst; and (3) a third step wherein catalyst obtained from the first step, the major portion of the catalyst being recycled between the first step and second step, is contacted with an oxygen-containing gas at a temperatur

Abstract: A process is described for cracking a heavy hydrocarbon to form a light oil and for producing hydrogen by the use of a catalyst containing at least 30 wt % Fe which comprises a first step wherein steam and heavy hydrocarbon are simultaneously contacted with the catalyst in a reduced state to produce hydrogen, cracked gases, and a cracked light oil, to oxidize the reduced-state catalyst, and to deposit coke on the catalyst; and a second step wherein the oxidized-state catalyst on which said coke is deposited is contacted with an oxygen-containing gas insufficient for achieving complete combustion of the coke, to thereby partially combust the coke and regenerate the catalyst to a reduced state.