Nippon Oil Corporation

Japan Cooperation Center Petroleum

Nippon Oil Company

Other

Nippon Mitsubishi Oil Corporation

Petroleum Energy Center

Saudi Arabian Oil Company

Japan Cooperation Ctr., Petroleum

Yuichiro Fujiyama

Toshiaki Okuhara

Shigeko Okuhara, Legal Representative

Akira Uchiura

Shozo Nishida

Masaru Ushio

Shunichi Yamamoto

Toru Morita

Yoneichi Ikeda

Christopher F Dean

Michiaki Adachi

Kozo Kamiya

Takata Okuhara

Syozo Nishida

Toshiyasu Okuhara

The fluid catalytic cracking process according to the present invention includes a first step of feeding a feedstock to a first fluid catalytic cracker, and catalytically cracking the feedstock in the first fluid catalytic cracker, so as to produce a fraction (LCO) having a boiling range of 221 to 343&#xb0; C. and having a total aromatic content of 40 to 80 volume %; and a second step of feeding an oil to be processed containing the fraction to a second fluid catalytic cracker having a reaction zone, a separation zone, a stripping zone, and a regeneration zone, and catalytically cracking the oil in the reaction zone of the second fluid catalytic cracker, in the presence of a cracking catalyst, at an outlet temperature of the reaction zone of 550 to 750&#xb0; C., a contact time between the oil and the catalyst of 0.1 to 1 second, and a catalyst/oil ratio of 20 to 40 wt/wt.

Fluid catalytic cracking process, and gasoline and liquefied petroleum gas obtained by the process

The production of light hydrocarbons consisting of ethylene, propylene, butylenes, and of gasoline is enhanced by introducing a heavy oil feedstream derived from an external source into an ancillary downflow reactor that utilizes the same catalyst composition as an adjacent FCC unit for cracking the heavy oil and withdrawing the desired lighter hydrocarbon reaction product stream from the downflow reactor and regenerating the catalyst in the same regeneration vessel that is used to regenerate the spent catalyst from the FCC unit. The efficiency of the recovery of the desired lighter olefinic hydrocarbons is maximized by limiting the feedstream to the downflow reactor to heavy oils that can be processed under relatively harsher conditions, while minimizing production of undesired by-products.

Ancillary cracking of heavy oils in conjunction with FCC unit operations

In processing of biomass by catalytic cracking in a fluidized catalytic cracker having a reaction zone, a separation zone, a stripping zone, and a regeneration zone, the feedstock oil containing the biomass is processed in the reaction zone using a catalyst containing 10 to 50 mass % of ultrastable Y-type zeolite under the conditions: outlet temperature of the reaction zone 580 to 680&#xb0; C., catalyst/oil ratio 10 to 40 wt/wt, reaction pressure 1 to 3 kg/cmG, and contact time of the feedstock oil with the catalyst in the reaction zone 0.1 to 1.0 sec, and the catalyst is then treated in the regeneration zone under the conditions: regeneration zone temperature 640 to 720&#xb0; C., regeneration zone pressure 1 to 3 kg/cmG, and exhaust gas oxygen concentration at the regeneration zone outlet 0 to 3 mol %.

Method of treating biomass, fuel for fuel cell, gasoline, diesel fuel, liquefied petroleum gas, and synthetic resin

A method of designing a gas-solid separator that has an inner cylinder having a closed lower end and an opened upper end, and extending in a vertical direction; an outer cylinder that coaxially covers the inner cylinder from the outside and has a gas vent port formed on the upper end side of the inner cylinder and communicating with an exterior; and a plurality of axially extending long holes formed a side surface on the lower end side of the inner cylinder in a circumferential direction, one of long side edge parts of each of the long holes being provided with a guide blade that protrudes outward and is inclined circumferentially so as to cover the long hole.

Method of designing gas-solid separator

To provide a mixing device capable of effectively mixing stock oil with a catalyst, while increasing the amount of throughput, the relations of 8.0&#x2267;Q&#xd7;(W/D)/(u+u), Q=300 to 2000 [kg/ms], W/D=0.2 to 0.5, u=5 to 300 [m/s], and u=5 to 300 [m/s] are satisfied when a mass flow per unit area of a moving bed is Q [kg/nes], the difference between an outer diameter and an inner diameter of the moving bed is W [m], an inner diameter of a reaction tube is D [m], a linear velocity of a horizontal component of the stock oil at a jet orifice of the internal stock oil injection nozzle u[m/s], and a linear velocity of a horizontal component of the stock oil at a jet orifice of the external stock oil injection nozzle u[m/s].

Mixing apparatus

A gas-solid separator has: an inner cylinderhaving a closed lower endand an opened upper end, and extending in a vertical direction; and an outer cylinderthat coaxially covers the inner cylinderfrom the outside and has a gas vent portformed on the upper end side and communicating with an exterior, wherein a plurality of axially extending long holesare formed on a side surface on the lower endside of the inner cylinderin a circumferential direction, one of long side edge parts of each of the long holesis provided with a guide bladethat protrudes outward and is inclined circumferentially so as to cover the long hole, and in a section of the outer cylinderthat surrounds the plurality of long holesof the inner cylinder, an inner diameter Dof a lower part is larger than an inner diameter Dof an upper part.

Gas-solid separator

A method for operating a gas-solid separator that has: an inner cylinderhaving a closed lower endand an opened upper end, and extending in a vertical direction; an outer cylinderthat coaxially covers the inner cylinderfrom the outside and has a gas vent portformed on the upper end side of the inner cylinder and communicating with an exterior; and a plurality of axially extending long holeshaving a length L[m] and formed on a side surface on the lower endside of the inner cylinderin a circumferential direction, one of long side edge parts of each of the long holes being provided with a guide bladethat protrudes outward and is inclined circumferentially so as to cover the long hole, wherein the length L of each long holeis defined such as to satisfy an expression of non-dimensional Stokes number St=(&#x3c1;d/(18&#x3bc;))&#xb7;U/L&#x2267;0.3, where U[m/s] represents a cross-sectional average linear velocity of a mixture of gas and solid particles that is supplied downward from the openingof the inner cylinder, &#x3c1;[kg/m] a particle density of the solid particles, d[m] an average particle diameter of the solid particles, and &#x3bc;[Pa&#xb7;s] a viscosity of the gas.

A gas-solid separator has: an inner cylinderhaving a closed lower endand an opened upper endand extending in a vertical direction; and an outer cylinderthat coaxially covers the inner cylinderfrom the outside and has a gas vent portformed on the upper end side of the inner cylinder and communicating with an exterior, wherein a plurality of axially extending long holesare formed on a side surface on the lower endside of the inner cylinderin a circumferential direction, one of long side edge parts of each of the long holesis provided with a guide bladethat protrudes outward and is inclined circumferentially so as to cover the long holeand a part between the long holesof the inner cylinderis concaved in a center direction of the inner cylinder

A process is disclosed for discharging and transferring upwardly fluidized particles from a dense fluidizing layer forming section to a high-velocity transferring section having a diameter which is smaller than that of the dense fluidizing fluidized layer forming section, wherein at least one intermediate cylindrical section is provided between the dense fluidizing fluidized layer forming section and the high-velocity transferring section. The process can decrease the degree of changes in the amount of particles to be discharged from the dense fluidizing layer forming section and transferred by the riser, thereby proving a stable and uniform transfer of the fluidized particles.

Process for discharging and transferring fluidized particles

An apparatus for mixing a fluid feed stock, such as a heavy oil, and particles of a catalyst for gasifying the heavy oil in a reactor, comprises the reactor having in the upper portion a circular port through which the particles are fed, a moving bed-forming section disposed on and in communication with the reactor for forming the particles into an annular or cylindrical high-velocity moving bed by dropping the particles downwardly into the reactor, while dispersing the particles radially, an external fluid feed section located so as to spray the feed stock over the entire upper outer periphery of the annular or cylindrical moving bed passing through the reactor, and an internal fluid-feed section located so as to spray the fluid over the entire upper inner periphery corresponding to the outer periphery of the annular moving bed.

Apparatus for mixing a fluid feedstock with particles

A device is disclosed for the quick separation between solid materials and reaction gaseous materials which comprises a vertically oriented inner cylindrical body with a closed end, which cylindrical body forms at the other end an inlet through which a mixture of the catalyst and the gaseous material is introduced and a substantially airtight outer cylindrical body disposed coaxially with said inner cylindrical body in surrounding relation thereto and forming at the upper portion a gas-discharging port communicating with the outside of the device and at the lower port a particle-discharging port communicating with the outside of the device, the inner cylindrical body being provided in the side surface with a plurality of elongated slits extending in the axial direction and spaced equally apart in the circumferential direction and a plurality of curved or flat guide vanes protruding outwardly from the proximity of the longitudinal edges of the slits at a certain angle with respect to the radial direction of the inner cylindrical body and extending vertically in a predetermined length. The device is increased in separation efficiency with a short residence time of the gaseous material even when the catalyst particles are contained in the mixture at a higher mix ratio.

Separation device

An object is to increase cracking rate of heavy fraction oils while producing a lessened amount of dry gases generated by the hydrogen transfer reaction and by the overcracking to obtain light fraction olefins in a high yield. A process for the fluid catalytic cracking of heavy fraction oils, which comprises steps of feeding the heavy fraction oils to a raw oil introducing portion provided at a reaction zone inlet; feeding a part of a regenerated catalyst taken out of a catalyst-regenerating zone to a catalyst introducing portion provided at a reaction zone inlet; and feeding another part of the regenerated catalyst taken out of the catalyst-regenerating zone to at least one catalyst introducing portion which is provided between the catalyst introducing portion provided at the reaction zone inlet and reaction zone outlet, the catalytic cracking in the reaction zone being carried out under conditions of a contact time of 0.1 to 3.0 sec. a reaction zone outlet temperature of 530 to 700.degree. C. and a catalyst/oil ratio of 10 to 50 wt/wt, thereby producing light fraction olefins.

Process for fluid catalytic cracking of heavy fraction oils

A process for the fluid catalytic cracking of oils, wherein an oil is brought into contact with catalyst particles using a fluid catalytic cracking reactor under the following conditions: a) a reaction zone outlet temperature of 580 to 630.degree. C., catalyst/oil ratio of 15 to 50 wt./wt., contact time of 0.1 to 3.0 sec.; b) a catalyst-concentrated phase temperature in the regenerating zone of 670 to 800.degree. C.; and c) a temperature of regenerated catalyst to be forwarded into the reaction zone of 610 to 665.degree. C.; thereby producing light fraction olefins. The process increases the cracking rate of heavy fractions of oils while producing a lessened amount of dry gases generated by the overcracking of light fractions to obtain light fraction olefins in a high yield.

Process for fluid catalytic cracking of oils

A process for removing iron impurities, inter alia iron or iron compounds, from petroleum oil distillation residues is disclosed in which a high gradient magnetic separator incorporates a pack of ferromagnetic fillers in the form of a generally flat or curved sheet-like strip. The ferromagnetic filler is a Fe--Cr alloy of a selected composition and the strip is of selected geometric characteristics such that the rate of removal of iron impurities can be maintained substantially at a maximum throughout the separation mode of operation prior to and after washing of the ferromagnetic filler.

Growing community of inventors

Yokohama, Japan

Yuichiro Fujiyama