30results about How to "High propylene content" patented technology

The inventive inorganic binder containing phosphorus and aluminum compounds comprises (by weight percentages) alumina 15-40, phosphorus pentoxide 45-80, and clay 1-40. The binder has P / Al weight ratio of 1-6, pH of 1-3, and solid content of 15-60 wt%. The preparation method includes mixing acid-soluble aluminum hydroxide and / or alumina, clay and deionized water; pulping into pulp having solid content of 15-45%; adding concentrated phosphoric acid into the pulp under stirring at P / Al weight ratio of 1-6; and reacting at 50-99 DEG C for 15-90 min. The preparation method can avoid binder solidification due to overheat caused by heat release of non-uniform local instantaneous intensive reaction of materials. The binder can improve wear resistance, activity and selectivity of FCC catalyst.

The invention relates to a catalytic conversion method for petroleum hydrocarbon. According to the method, raw oil contacts a catalyst in a reactor to carry out a reaction, wherein the catalyst is rich in mesoporous zeolite; a cracking reaction is performed under the following conditions: a reaction temperature is 500-750 DEG C, weight hourly space velocity is 100-800 h<-1>, reaction pressure is 0.10-1.0 MPa, a weight ratio of the catalyst to the raw oil is 1:100, a weight ratio of water vapour to the raw oil is 0.05:1.0; the spent catalyst and the reaction oil gas are separated; the spent catalyst is subjected to regeneration, and returns to the reactor, the reaction oil gas is separated to obtain a product, wherein the product comprises ethylene, propylene, propane, butane and arene-rich catalytic gasoline; the catalytic gasoline is subjected to selective hydrogenation, and enters an arene extraction apparatus to separate to obtain the target product of light arene; the raffinate oil, the propane and the butane are subjected to steam cracking to further produce ethylene and propylene. With the method provided by the present invention, the yields of the ethylene and the propylene are respectively 20.31 wt% and 31.67 wt%, the yield of BTX is 24.39 wt%.

The invention discloses a process and a device for processing and preparing hydrocarbon by utilizing liquefied gas. The process comprises the processes of cracking reaction, absorption and stabilization, aromatization reaction, gas separation raw material gas stripping concentration and aromatic hydrocarbon purification. The device comprises a cracking reaction system, an absorption and stabilization system, an aromatization reaction system, a gas separation raw material gas stripping concentration system and an aromatic hydrocarbon purification system. The process and the device have the advantages that the energy consumption is low, and after the process is adopted, a deisobutanizer stops running, 90 kilograms of standard coals consumed by a carton-4 raw material per ton are treated, and 48.5 percent of energy is saved; gas separation raw material gas propylene is high in content and is improved from 15 percent to 50 percent in mass fraction; the requirements on equipment and heat energy are low and are easily realized; and the device is simple in process, is easy in operation and control and stable in running.

The invention discloses a method for producing propane by hydrogen conversion of light hydrocarbons. The light hydrocarbon raw material, hydrogen-rich gas and circulating light hydrocarbons are heated to the reaction temperature, and catalytic cracking reaction occurs under the condition of an acidic catalyst. The reaction products are cooled and fractionated to obtain dry gas, propane, and aromatic gasoline components respectively. Unreacted light components are obtained. The hydrocarbon feedstock, hydrogen-rich gas and recycle light hydrocarbons are returned to the reactor to continue the reaction. On the one hand, the present invention uses light alkanes as raw materials, which can effectively utilize a large amount of excess light alkanes in refineries; Increase feedstock conversion and propane yield.

The invention relates to the field of organic matter recovery from gas and discloses a device and a method for recovering C2 from catalytic dry gas. The device comprises a C4 absorption tower, a C4 desorption tower and a second gasoline absorption tower which are connected sequentially as well as a first gasoline absorption tower and a gasoline stabilization tower which are connected. The method comprises the following steps: C4 is contacted with the catalytic dry gas, so that heavy components of C2 or higher in the catalytic dry gas are absorbed; the absorbed C4 and heavy components of C2 orhigher are subjected to first rectification, and crude C2 and C4 are obtained by separation; gasoline is contacted with crude C2, then heavy components in crude C2 are absorbed, and C2 is further separated out; remaining gasoline-containing components are contacted with unabsorbed light components, C4 entrapped in the light components is absorbed, a mixture of absorbed C4 and gasoline is subjectedto second rectification, and C4 and gasoline are separated and reused to previous steps respectively. With adoption of the method, C2 can be recovered from the catalytic dry gas effectively, and content of propylene, ethane and C4 in a product is lower.

The invention relates to a catalytic cracking assistant of highly productive isomeric low-carbon olefin as well as a preparation method and application thereof. The catalytic cracking assistant of the highly productive isomeric low-carbon olefin is prepared from the following components by dry basis base on the total weight of the catalytic cracking assistant: 15 to 45 weight percent of alkali-modified ZSM-5 molecular sieve; 1 to 20 weight percent of mesoporous ZSM-5 molecular sieve; 1 to 10 weight percent of beta-zeolite; 3 to 25 weight percent of P205; 3 to 25 weight percent of inorganic oxide; and the balance of clay. The catalytic cracking assistant of the highly productive isomeric low-carbon olefin can accelerate shape-selective isomerization cracking reaction of gasoline composition of C8 or above in catalytic cracking gasoline, can synchronously improve the productivity of propylene, isobutene and isoamylene, improve propylene content in liquefied gas increment (delta propylene / delta liquefied gas), and co-produce gasoline with high-octane rating.

The invention discloses a hydrocarbon oil cracking method which comprises that: in a riser reactor comprising a plurality of reaction areas, the hydrocarbon oil raw material and the cracking catalyst are made a contact reaction in each reaction area under the condition of cracking reaction, the catalyst is separated from the reaction product to obtain the cracking product and spent catalyst, at least partial spent catalyst is regenerated to obtain the semi-regenerated catalyst and the regenerated catalyst, wherein, the reaction areas comprise at least one middle reaction area and at least one upper reaction area, the upper reaction area is positioned above the middle reaction area; the inferior heavy raw material and the semi-regenerated catalyst are imported in the middle reaction area to allow the heavy raw material to contact the semi-regenerated catalyst; the heavy raw material and the regenerated catalyst are imported in the upper reaction area to allow the heavy raw material to contact the regenerated catalyst. At least one item of the carbon residue content, the content of metal nickel and vanadium, the bitumencarb content and the basic nitrogen content of the inferior heavy raw material is higher than that of the heavy raw material. The method can optimize the cracking conditions of the hydrocarbon oil and improve the distribution of products.

The invention relates to the field of catalytic cracking reactions, and discloses a catalytic cracking method and a catalytic cracking system. The method comprises: under the action of a pre-lifting medium, the catalytic cracking raw material is subjected to a catalytic cracking reaction in a riser reactor, the gas phase is separated from the reaction product, and the gas phase is injected into an absorption tower for treatment, and the gas phase is injected from the top of the absorption tower Lean gas is collected and at least a portion of said lean gas is recycled as a pre-lift medium. The catalytic cracking system includes a reaction device equipped with a riser reactor and an absorption tower, the gas phase outlet at the top of the reaction device communicates with the gas phase inlet of the absorption tower, and the lean gas outlet at the top of the absorption tower communicates with the lift The pre-lift medium inlet at the bottom of the tube reactor communicates. By adopting the catalytic cracking method and the catalytic cracking system of the present invention, the gas phase load of the reabsorption tower can be reduced, the absorption effect can be effectively improved, and the propylene component carried in the dry gas can be reduced.

The invention provides a method for combining catalytic cracking and gasoline hydrogenation, which comprises the following steps: subjecting catalytic cracking raw materials to catalytic cracking reaction, and then performing fractionation, separation, analysis, absorption and stabilization in sequence to obtain dry gas, liquefied gas, Light naphtha, diesel oil and oil slurry; 60-70wt% of light naphtha and gasoline are sequentially separated by gasoline hydrogenation reaction and gasoline hydrogenation to obtain external materials and reuse materials; distillation range of light naphtha Control the C3+C4 content <1wt%, dry point <70℃; the distillation range of the recycled material controls the initial boiling point>40℃, the final boiling point 90~101℃; the light naphtha is 30%~40℃ % and recycled materials are returned to continue the catalytic cracking reaction. In the method, 30% to 40% of the light naphtha is subjected to catalytic cracking reaction together with the recycled material and the catalytic cracking raw material, so that the liquefied gas yield and the propylene content in the liquefied gas are both improved, and the ethylene content in the dry gas is also significantly increased.

The invention relates to a catalytic cracking additive for increasing yield rates of propylene and isopentene as well as a preparation method and application thereof. The catalytic cracking additive for the increasing yield rates of propylene and isopentene is prepared from the following components in percentage by weight based on the dry basis: 15 to 45 wt% of alkaline-modified ZSM-5 molecular sieve, 1 to 20 wt% of USY molecular sieve, 1 to 10 wt% of beta-zeolite, 3 to 25 wt% of P2O5 (phosphorus pentoxide), 3 to 25 wt% of inorganic oxide, and the balance of clay. The catalytic cracking additive for increasing the yield rates of propylene and isopentene has the advantages that the selective heterogenous cracking reaction of C8 or above gasoline components in gasoline can be promoted to catalyze and crack, the yield rates of propylene and isopentene are synchronously increased, the content of propylene (delta propylene / delta liquefied gas) in the liquefied gas increment is increased, and the gasoline with high octane number is jointly produced.

The invention discloses a combined process for treating residual oil. Boiling bed residual oil hydrotreatment, delayed coking, wax oil hydrotreatment and catalytic cracking are organically combined in the method. The method concretely comprises the following steps of: enabling a liquid-phase product obtained after residual oil raw materials are subjected to boiling bed hydrotreatment to directly enter a coking fractional distillation column to be in countercurrent contact with oil gas generated through coking, and then, carrying out fractional distillation to obtain a wax oil fraction, and enabling the wax oil fraction to enter a wax oil hydrotreatment device, wherein the liquid-phase product is not subjected to fractional distillation; enabling the obtained liquid-phase product as a raw material to enter a catalytic cracking unit for treating; enabling circulating oil obtained through the fractional distillation of the coking fractional distillation column to return to a delayed coking unit; generating gasoline and diesel products by the coking fractional distillation column; and carrying out catalytic cracking and fractional distillation to obtain liquefied gas, gasoline and diesel products. Compared with the prior art, the combined process has the advantages that a hydrogenization fractional distillation column can be omitted, the investment cost can be reduced, the coking and catalytic cracking raw material sources are expanded, and the coked and catalyzed light oil yield is increased; and meanwhile, the reaction heat energy is sufficiently utilized, and the production energy consumption is reduced.

A catalyst for catalytic cracking of a hydrocarbon oil can produce a gasoline fraction having a high octane number in high yield while suppressing an increase in yield of a heavy distillate, and produce LPG having a high propylene content in high yield. The catalyst includes a specific amount of a granulated catalyst A that includes a zeolite having a sodalite cage structure, silicon derived from a silica sol, phosphorus and aluminum derived from mono aluminum phosphate, a clay mineral, and a rare-earth metal, and a specific amount of a granulated catalyst B that includes a pentasil-type zeolite, the ratio of the mass of phosphorus and aluminum derived from mono aluminum phosphate included in the granulated catalyst A to the mass of the pentasil-type zeolite included in the granulated catalyst B being 0.015 to 3000.

The invention discloses a device for processing hydrocarbons by using liquefied gas, including a cracking reaction system, an absorption stabilization system, an aromatization reaction system, a gas separation raw material gas concentration system, and an aromatics purification system; The isobutane tower stopped running, processing 90kg of standard coal per ton of C4 raw material, saving 48.5% of energy consumption, high content of propylene in the raw material gas, increased from 15% of the original mass fraction to 50%, low requirements for equipment and heat energy , easy to implement, simple device process, easy to operate, low energy consumption, and stable operation.