89results about How to "Reduced dry gas yield" patented technology

The invention relates to an aromatization catalyst comprising two molecular sieves of ZSM-5 and MCM-22, wherein the molecular sieves are in a hydrogen type, the total weight percentage of the two molecular sieves is 10-90 in the catalyst, the weight rate of the molecular sieve ZSM-5 and the molecular sieve MCM-22 is 90:10-50:50, the molecular sieve ZSM-5 is modified by phosphorus and a rare-earth element, and the molecular sieve MCM-22 is modified by zinc. The preparation method of the aromatization catalyst comprises the following steps of: firstly, modifying the two molecular sieves respectively; and then preparing the catalyst. The aromatization catalyst has higher aromatic yield, lower dry-gas yield and higher acrylic yield when being used for aromatizing n-alkane, cyclane, naphtha, and the like.

The invention discloses a catalytic conversion method for preparing propylene and high octane gasoline. Raw oil of different cracking properties enters different reaction regions of a first riser reactor to contact with catalytic cracking catalysts for carrying out cracking reactions so as to separate a spent catalysts from reaction oil gas; the reaction oil gas is separated for obtaining a product comprising the propylene, gasoline and a re-cracking raw material, wherein the re-cracking raw material is transmitted into a second riser reactor to contact with hot regenerated catalysts for carrying out catalytic conversion; and after the spent catalysts in the two riser reactors are burned in a same regenerator, the spent catalysts are respectively returned to the two riser reactors. In themethod, the yields of the propylene and the gasoline are obviously increased; the octane value of the gasoline is also obviously improved. Under the condition of largely increasing the yield of the propylene, the yield of dry gas is obviously reduced by more than 80% by weight.

The invention discloses a treatment method for improving the selectivity of a catalytic cracking catalyst, which comprises the following steps: filling a fresh catalyst into a phase fluidized bed, contacting the fresh catalyst with aging medium containing water vapor, aging under a certain hydrothermal condition to obtain an aged catalyst; and adding the aged catalyst into an industrial catalytic cracking device. In the method, the activity and selective distribution of the catalyst in the catalytic cracking device are more uniform to obviously improve the selectivity of the catalytic cracking catalyst, thereby obviously reducing dry gas productivity and coke productivity.

The invention provides a light hydrocarbon aromatization catalyst which comprises a composite carrier and modified components, wherein the modified components comprise the following compositions which are calculated based on the carrier in mass percentage by mass percent: 1.0-10.0% of ZnO, 0.5 to 10.0% of rare earth oxide; the composite carrier comprises 10 to 90% of H zeolite socony mobile-5 (HZSM-5) and 10 to 90% of silica. The catalyst preparation is simple and has high aromatization activity and selectivity on light hydrocarbon, and the carbon-depositing amount of the catalyst after reaction is less. With mixed C4 as a raw material for aromatization reaction, the yield of aromatics reaches 50 % by mass and the one-way service life of the catalyst lasts as long as 700 hours.

The invention discloses a catalytic conversion method for producing propylene. Raw material which is difficult for cracking is contacted with a thermal regeneration catalyst, and cracking reaction is carried out under the conditions that the reaction temperature is 600 DEG C to 750 DEG C, the weight hourly space velocity is 100-800h<-1>, the reaction pressure is 0.10MPa to 1.0MPa, the weight ratio of the catalytic cracking catalyst and raw material is 30 to 150, and the weight ratio of steam and raw material is 0.05 to 1.0. The reaction material flow is mixed with raw oil which is easy to be cracked, and cracking reaction is carried out under the conditions that the reaction temperature is 450 DEG C to 620 DGE C, the weight hourly space velocity is 0.1-100 h<-1>, the reaction pressure is 0.10MPa to 1.0MPa, the weight ratio of the catalytic cracking catalyst and raw material is 1.0 to 3.0, and the weight ratio of the steam and raw material is 0.05 to 1.0; then a spent catalyst and reaction oil gas are separated, the spent catalyst returns to a reactor after regeneration, and the target products comprising propylene and recracking raw material are obtained by separating the reaction oil gas. By adopting the method of the invention, the yield of the propylene and the selectivity of the propylene in liquefied gas are increased greatly, moreover, the yield of dry gas is reduced obviously.

The invention provides a catalyst for producing propane and high octane number gasoline by using butane. The catalyst comprises, by mass, 20-85% of mesoporous Si-Al zeolite and 15-80% of a binder, and has an alpha value of 25-50. With the catalyst of the present invention, butane can be converted into propane under a certain reaction condition, and a high octane number gasoline blending component is by-produced, wherein the produced propane is used for ethylene cracking raw materials and other chemical industry uses, and the high octane number gasoline blending component is used for blending catalytic cracking gasoline so as to substantially reduce olefin content.

The invention provides a high treatment capacity feed atomizing nozzle, and belongs to the field of petrochemical equipment. A combined cyclone, a multi-point gas injection structure and a spray-head with a porous impinging structure are adopted; and a hard alloy surfacing structure is adopted at orifices. The nozzle is suitable for feed atomizing nozzles of heavy oil FCC devices with the yield of 3,500,000-6,000,000 tons/year, the treatment capacity of a single nozzle is 60-100t/h, and a defect that the dimension of the nozzle is changed due to high treatment capacity so as to cause low atomizing effect is improved; meanwhile, the nozzle has the atomized particle size in a range of 60+/-10 mu m, the liquid layer on the injected sector surface is distributed uniformly, the yield of light oil is high, the productivity of dry gas is low, and the coking in the tubes is improved; besides, the steam consumption is low, and the gas/liquid ratio is between 3 and 6 percent (raw materials). In addition, the injecting speed of the nozzle is medium, a phenomenon that a catalyst is broken cannot occur in the production, and the nozzle has high wear resistance and the service life of more than 5 years.

The invention discloses a catalytic conversion method for preparing propylene and high octane gasoline. After entering different reaction regions of a first riser reactor, raw oils with different cracking performances are contacted with catalytic cracking catalyst to carry out cracking reaction so as to separate a spent catalyst and reaction oil gas, wherein the spent catalyst subject to steam stripping enters a first regenerator to be regenerated by scorching and returns to a first riser, and a product containing the propylene, the gasoline and recracking raw materials is obtained through separation of the reaction oil-gas, wherein the recracking raw materials are sent into a second riser reactor and are contacted with thermal regeneration catalyst to carry out catalytic conversion, and the spent catalyst returns to the second riser reactor after coke burning regeneration in a second regenerator. In the method, the yield of the propylene and the yield of the gasoline are obviously increased, and the gasoline octane number is obviously improved; and under the condition that the propylene yield is dramatically increased, the dry gas yield is obviously lowered by above 80 weight percent.

The invention discloses a catalytic cracking method. The method comprises steps of: introducing dry gas and C4 hydrocarbon into a middle and lower part of a stripping section of a sub-precipitator to react with a gasoline coked catalyst; introducing the oil gas after reaction into a sub-fractionating column; introducing part of the coked catalyst treated with steam stripping into a regenerator for regeneration, and introducing the other part of the coked catalyst treated with steam stripping into a pre-lifting mixer and mixing with a regenerative agent from the regenerator; and returning the mixed catalyst to a heavy oil riser reactor. The method can reduce yield of dry gas by 0.3-1.5 percentage, reduce yield of liquefied gas (not including propylene) by 2.0-8.0 percentage, increase yield of gasoline by 1-4 percentage, and increase yield of propylene by 0.5-2.5 percentage.

The invention relates to a catalytic conversion method capable of improving product selectivity. The method comprises the step of carrying out reaction on a raw material oil and a carbon-containing catalyst in a reactor, and is characterized in that the carbon content in the catalyst is 0.15-0.8wt%. The invention relates to the catalytic conversion method capable of improving product selectivity, particularly a method capable of converting a heavy raw material into a high-value product such as gasoline, greatly reducing the yield of dry gas and coke, and realizing the high-efficiency utilization of petroleum resources.

The invention relates to a method for preparing BTX and co-producing tetramethylbenzene from C9<+> heavy aromatic hydrocarbons. The method comprises: carrying out catalytic cracking conversion on C9<+> heavy aromatic hydrocarbons to obtain a first-stage hydrocarbon mixing product using BTX and trimethylbenzene as main components, and separating respectively with an ethane removing tower, a butane removing tower, a hexane removing tower, a BTX removing tower and a trimethylbenzene removing tower to obtain dry gas, liquefied gas, C5-C6 non-aromatic hydrocarbons, BTX, trimethylbenzene and C10<+> heavy aromatic hydrocarbons, wherein the dry gas, the liquefied gas, the C5-C6 non-aromatic hydrocarbons and the BTX are adopted as products; carrying out a reaction on the trimethylbenzene and a certain amount of methanol to obtain a tetramethylbenzene-rich second-stage mixing product, and separating the products to obtain dry gas, wastewater and liquid-state hydrocarbons, wherein the liquid-state hydrocarbon products return to the ethane removing tower so as to be separated; and carrying out crystallization separation on the C10<+> heavy aromatic hydrocarbons to obtain tetramethylbenzene and a heavy component residue liquid, wherein the tetramethylbenzene and the part of the heavy component residue liquid are adopted as the product, and the remaining heavy component residue liquid return to a catalytic cracking reactor. According to the present invention, with the method, the moving bed non-hydrogen cracking and the tetramethylbenzene preparation using trimethylbenzene alkylation are compounded, such that the BTX is produced at a maximum while the high added value tetramethylbenzene can be co-produced.

A low-quality oil catalytic cracking process is characterized in that light diesel produced from the low-quality oil by catalytic cracking is partially or entirely reprocessed to correspondingly reduce the feed amount of fresh materials. As a result, the yield of light diesel is reduced greatly or even reduced to zero relevant to fresh catalytic material; the yields of liquefied gas and gasoline are improved greatly and the propylene yield is improved correspondingly; and the slurry oil can be partially reprocessed so that the light oil yield is improved greatly in comparison with the process for withdrawing all of the slurry oil. Since the yield of catalytic cracked diesel with low cetane number is reduced greatly, qualified commodity diesel can be prepared from straight-run diesel more easily by refinery plant.

The invention relates to a molecular sieve-containing alumina pellet and a preparation method thereof. The preparation method comprises: (1) preparation of a mixed sol: mixing pseudo-boehmite, urea and deionized water to obtain an aluminum hydroxide suspension liquid, adding a first acid solution to the aluminum hydroxide suspension liquid, carrying out first peptization to obtain an alumina sol,mixing the alumina sol and a molecular sieve, adding a second acid solution, and carrying out second peptization to obtain a mixed sol; and (2) preparation of molecular sieve-containing alumina pelletby hot oil column molding: mixing the mixed sol obtained in the step (1) and hexamethylenetetramine, adding into a hot oil column in a dropwise manner, molding to obtain pellets, taking out the molded pellets, washing, drying, and roasting to obtain the molecular sieve-containing alumina pellet. According to the present invention, the obtained molecular sieve-containing alumina pellet has characteristics of high molecular sieve content and high crushing strength.

A catalyst for preparing oil products from used plastics is prepared from zeolite, components A, B and M, Na, Ca and Fe through washing zeolite with the solution of ammonium oxide, proportionally mixing with others, adding alpha-AlO(OH) powder and sodium silicate, stirring, granulating and calcining at 350-750 deg.C. Its advantages are low cost, long service life, and high output rate and quality of resultant oil products.

Belonging to the technological field of petroleum refining, the invention relates to a catalytic cracking unit stripper, which includes a stripper cylinder. Stripping baffles and stripping steam distributors are disposed in the stripper cylinder in the axial direction from top to bottom. The stripper is characterized in that: the stripping baffles are spiral stripping baffles and fixed on the inner wall of the stripper cylinder, and the spiral stripping baffles are provided with gas distribution holes. With the catalytic cracking unit stripper provided by the invention, a catalyst and stripping steam can be more uniformly distributed in the stripper, the gas-solid contact time is prolonged, the gas-solid countercurrent and cross flow contact can be increased, channeling in the catalyst in the stripper can be avoided, and the gas-solid backmixing degree in the stripper can be reduced, thereby realizing complete gas-solid contact and improving the contact efficiency and mass transfer efficiency of the catalyst and stripping steam.