Abstract: A system for catalytic cracking of hydrocarbon oils has a catalytic cracking reactor, a catalyst separation device, an optional reaction product separator, and a regenerator. A catalytic cracking reactor has a dilute-phase transport fluidized bed and a fast fluidized bed connected in series for reaction. In the fast fluidized bed, the axial solid fraction ? of the catalyst is controlled within the range of about 0.1 to about 0.2. When used for catalytic cracking of hydrocarbon oil feedstocks, particularly heavy feedstock oils, the process and system show lower yields of dry gas and coke, and good product distribution.

Abstract: A process for catalytic cracking of hydrocarbon oils includes the step of contacting a hydrocarbon oil feedstock with a catalytic cracking catalyst in a reactor comprising a dilute-phase transport fluidized bed and a fast fluidized bed connected in series for reaction. In the fast fluidized bed, the axial solid fraction ? of the catalyst is controlled within the range of about 0.1 to about 0.2. When used for catalytic cracking of hydrocarbon oil feedstocks, particularly heavy feedstock oils, the process and system show lower yields of dry gas and coke, and good product distribution.

Abstract: A process includes: cutting a hydrocarbon-containing feedstock oil into a light distillate oil and a heavy distillate oil; introducing the light distillate oil and a first catalyst into a down-flow reactor to produce a stream; subjecting the stream to a gas-solid separation to produce a first reaction hydrocarbon product and a first spent catalyst; or, introducing the stream into a fluidized bed reactor, and then subjecting to a gas-solid separation to produce a second reaction hydrocarbon product and a second spent catalyst; introducing a continuous catalyst, the heavy distillate oil and a second catalyst into an up-flow reactor, and then subjecting to a gas-solid separation to produce a third reaction hydrocarbon product and a third spent catalyst; separating out lower carbon olefins and light aromatics from reaction hydrocarbon products, separating out a light olefin fraction, and returning the light olefin fraction to the fluidized bed reactor or the up-flow reactor.

Abstract: A process for the catalytic cracking of hydrocarbon oils includes the step of contacting a hydrocarbon oil feedstock with a catalytic cracking catalyst in a reactor having one or more fast fluidized reaction zones for reaction. At least one of the fast fluidized reaction zones of the reactor is a full dense-phase reaction zone, and the axial solid fraction ? of the catalyst is controlled within a range of about 0.1 to about 0.2 throughout the full dense-phase reaction zone. When used for catalytic cracking of hydrocarbon oils, particularly heavy feedstock oils, the process, reactor and system show a high contact efficiency between oil and catalyst, a selectivity of the catalytic reaction, an effectively reduced yield of dry gas and coke, and an improved yield of high value-added products such as ethylene and propylene.

Abstract: In a method and system for treating a catalytic cracking gasoline, a catalytic cracking process, or a plant employs a fluidized reactor to carry out hydrodealkylation treatment on a catalytic cracking oil gas or catalytic cracking gasoline, so that heavy aromatics present therein can be efficiently converted into light olefins and light aromatics. The method and system can improve the yield of light olefins, allow a long-period stable operation, relieve the contradiction between supply and demand of light aromatics, and solve the problem of high content of heavy aromatics that have low value and are difficult to be utilized in aromatics present in oil gas from catalytic cracking units.

Abstract: A method for producing light aromatics, includes the steps of: i) contacting a feedstock comprising heavy aromatic(s) with a catalyst in a fluidized reactor for aromatics lightening reaction in the presence of hydrogen to obtain a product rich in C6-C8 light aromatic(s) and a spent catalyst, wherein the heavy aromatic is one or more selected from C9+ aromatics; ii) separating the resulted product rich in C6-C8 light aromatic(s) to obtain hydrogen, a non-aromatic component, C6-C8 light aromatic(s) and a C9+ aromatic component; and iii) recycling at least a part of the C9+ aromatic component to the fluidized reactor. The method has strong adaptability to feedstocks and high flexibility in operation and allows a long-period stable operation. The method can produce high-value light aromatics from heavy aromatics that are difficult to be treated and utilized.

Abstract: A process for producing light olefins from inferior oils includes the steps of: subjecting an inferior oil to a thermal conversion reaction in the presence of hydrogen to obtain a conversion product; separating the conversion product to obtain a first separated product; separating the first separated product to obtain an upgraded oil and a pitch; subjecting the upgraded oil to hydro-upgrading to obtain a hydro-upgraded oil; separating the hydro-upgraded oil to obtain a hydro-upgraded heavy oil; and subjecting the hydro-upgraded heavy oil to catalytic cracking to obtain a catalytic cracking product comprising a light olefin.

Abstract: A process for catalytic cracking of hydrocarbon oils includes the step of contacting a hydrocarbon oil feedstock with a catalytic cracking catalyst in a reactor comprising a dilute-phase transport fluidized bed and a fast fluidized bed connected in series for reaction. In the fast fluidized bed, the axial solid fraction c of the catalyst is controlled within the range of about 0.1 to about 0.2. When used for catalytic cracking of hydrocarbon oil feedstocks, particularly heavy feedstock oils, the process and system show lower yields of dry gas and coke, and good product distribution.

Abstract: The present disclosure provides a colored glass and a preparation method thereof. The colored glass comprises a glass substrate, layer Aed structure and a Ti alloy layer, wherein the layered structure and the Ti alloy layer are laminated on the surface of the glass substrate; the layered structure comprises alternately stacked layer A and layer B; the layer A is a SiC or NiO layer; the layer B is an MN layer, a GaN layer, a ZrO2 layer or an Nb2O5 layer; the layer A is in contact with the glass substrate, the layer B is in contact with the Ti alloy layer. The color of the glass is controlled by adjusting the thickness of the layer A and the layer B in the layered structure. The Ti alloy layer has high reflectivity, which can make the colored glass bright in color, and has a certain protective and corrosion-resistant effect.

Abstract: A process for the catalytic cracking of hydrocarbon oils includes the step of contacting a hydrocarbon oil feedstock with a catalytic cracking catalyst in a reactor having one or more fast fluidized reaction zones for reaction. At least one of the fast fluidized reaction zones of the reactor is a full dense-phase reaction zone, and the axial solid fraction ? of the catalyst is controlled within a range of about 0.1 to about 0.2 throughout the full dense-phase reaction zone. When used for catalytic cracking of hydrocarbon oils, particularly heavy feedstock oils, the process, reactor and system show a high contact efficiency between oil and catalyst, a selectivity of the catalytic reaction, an effectively reduced yield of dry gas and coke, and an improved yield of high value-added products such as ethylene and propylene.

Abstract: Disclosed is a process and system for upgrading low-quality oils. The upgrading process comprises: (1) subjecting a low-quality oil to a conversion reaction in the presence of hydrogen and optionally in the presence of a conversion catalyst to obtain a conversion product, (2) processing the conversion product to obtain a first processed product, wherein the first processed product comprises a specific amount of a special component, and (3) subjecting the first processed product to extraction separation to obtain an upgraded oil and a pitch. The upgrading process and the upgrading system have the advantages of stable operation, high upgrading efficiency, environmental friendliness, low coke yield or high yield of upgraded oil.

Abstract: A process for producing catalytic cracking gasoline includes the following steps: i) subjecting a heavy feedstock oil to a catalytic cracking reaction in the presence of a first catalytic cracking catalyst to obtain a first reaction product; ii) subjecting a hydrogenated cycle oil to a catalytic cracking reaction in the presence of a second catalytic cracking catalyst to obtain a second reaction product; iii) separating a mixture of the first reaction product and the second reaction product to obtain a catalytic cracking gasoline and a catalytic cracking light cycle oil; iv) subjecting the catalytic cracking light cycle oil or a fraction thereof to hydrogenation to obtain a hydrogenated product; and v) recycling the hydrogenated product to the step ii) as the hydrogenated cycle oil.

Abstract: A catalytic cracking process includes the following steps: i) subjecting a heavy feedstock oil to flail catalytic cracking; ii) separating the catalytic cracking reaction product obtained from step i) to obtain a catalytic cracking gasoline and a catalytic cracking light cycle oil; iii) splitting the catalytic cracking gasoline to obtain a light gasoline fraction, a medium gasoline fraction and a heavy gasoline fraction; iv) subjecting the catalytic cracking light cycle oil to hydrogenation to obtain a hydrogenated light cycle oil); v) mixing a portion of the light gasoline fraction with at least a portion of the hydrogenated light cycle oil to obtain a mixed fraction; vi) subjecting the mixed fraction to catalytic cracking; and vii) subjecting a portion of the medium gasoline fraction to flail catalytic cracking. The process is capable of producing more catalytic cracking gasoline, reducing the olefin content of the catalytic cracking gasoline, and increasing its octane number.

Abstract: Disclosed is a process and system for upgrading low-quality oils. The upgrading process comprises: (1) subjecting a low-quality oil to a conversion reaction in the presence of hydrogen and optionally in the presence of a conversion catalyst to obtain a conversion product, (2) processing the conversion product to obtain a first processed product, wherein the first processed product comprises a specific amount of a special component, and (3) subjecting the first processed product to extraction separation to obtain an upgraded oil and a pitch. The upgrading process and the upgrading system have the advantages of stable operation, high upgrading efficiency, environmental friendliness, low coke yield or high yield of upgraded oil.

Abstract: The present disclosure relates to a process for producing catalytic cracking gasoline comprising the following steps: i) subjecting a heavy feedstock oil to a catalytic cracking reaction in the presence of a first catalytic cracking catalyst to obtain a first reaction product; ii) subjecting a hydrogenated cycle oil to a catalytic cracking reaction in the presence of a second catalytic cracking catalyst to obtain a second reaction product; iii) separating a mixture of the first reaction product and the second reaction product to obtain a catalytic cracking gasoline and a catalytic cracking light cycle oil; iv) subjecting the catalytic cracking light cycle oil or a fraction thereof to hydrogenation to obtain a hydrogenated product; and v) recycling the hydrogenated product to the step ii) as the hydrogenated cycle oil. The present disclosure also relates to a catalytic cracking system for carrying out the process.

Abstract: The present disclosure relates to a catalytic cracking process comprising the following steps: i) subjecting a heavy feedstock oil to a catalytic cracking reaction to obtain a catalytic cracking reaction product; ii) separating the catalytic cracking reaction product to obtain a catalytic cracking gasoline and a catalytic cracking light cycle oil; iii) splitting the catalytic cracking gasoline to obtain a light gasoline fraction, a medium gasoline fraction and a heavy gasoline fraction; iv) subjecting the catalytic cracking light cycle oil to hydrogenation to obtain a hydrogenated light cycle oil); v) mixing a portion of the light gasoline fraction with at least a portion of the hydrogenated light cycle oil to obtain a mixed fraction; vi) subjecting the mixed fraction to a catalytic cracking reaction; and vii) subjecting a portion of the medium gasoline fraction to a catalytic cracking reaction.

Abstract: Disclosed is a process for producing light olefins. In the process for producing light olefins by continuously bringing an alkane feedstock and a catalyst into contact to subject to a dehydrogenation reaction, the reaction pressure P of the dehydrogenation reaction is made 0.6-2 MPa and the volume space velocity H of the dehydrogenation reaction is made 500-1000 h?1. The light olefins production process of the present invention is simple and continuous in operation and has the characteristics of low investment, significant increase in yield of light olefins and high safety.

Abstract: Disclosed is a process for producing light olefins. In the process for producing light olefins by continuously bringing an alkane feedstock and a catalyst into contact to subject to a dehydrogenation reaction, the reaction pressure P of the dehydrogenation reaction is made 0.6-2 MPa and the volume space velocity H of the dehydrogenation reaction is made 500-1000 h?1. The light olefins production process of the present invention is simple and continuous in operation and has the characteristics of low investment, significant increase in yield of light olefins and high safety.

Abstract: The present invention provides a catalytic cracking catalyst, processing method and use thereof. When the catalyst is added into a commercial catalytic cracking unit, it has an initial activity of not higher than 80, preferably not higher than 75, more preferably not higher than 70, a self-balancing time of 0.1-50 h, and an equilibrium activity of 35-60. Said method enables the activity and selectivity of the catalyst in the catalytic cracking unit to be more homogeneous and notably improves the selectivity of the catalytic cracking catalyst, so as to obviously reduce the dry gas and coke yields, to sufficiently use steam and to reduce the energy consumption of the FCC unit.

Abstract: A catalytic conversion process uses a catalytic cracking catalyst having a relatively homogeneous activity containing mainly large pore zeolites in a catalytic conversion reactor. The reaction temperature, residence time of oil vapors and weight ratio of the catalyst/feedstock oil are sufficient to obtain a reaction product containing from about 12 to about 60% by weight of a fluid catalytic cracking gas oil relative to the weight of the feed stock oil and containing a diesel. The reaction temperature ranges from about 420° C. to about 550° C. The residence time of oil vapors ranges from about 0.1 to about 5 seconds. The weight ratio of the catalytic cracking catalyst/feedstock is about 1-about 10.