139 results about "Cracking" patented technology

The present application relates to the field of catalytic cracking of hydrocarbons, in particular to a silicon-aluminum molecular sieve catalyst, a preparation method and application thereof, and aims to provide a method for synthesizing a silicon-aluminum molecular sieve by mechanical ball milling, in which full-silicon molecular sieves are synthesized, and aluminum elements are selectively added into the full-silicon molecular sieves, so that the synthesized silicon-aluminum molecular sieve has appropriate acidity and good pore structure, and the ball milling process can form more defects on the outer surface of the full-silicon molecular sieve, thereby increasing the positioning space of aluminum.

The present application relates to a kind of Y type molecular sieve catalytic material for improving gasoline yield and selectivity and its preparation method, Y type molecular sieve catalytic material is obtained by the hydrothermal crystallization of reactive microspheres containing zirconium, reactive microspheres containing zirconium contain 85-99.9 wt% alumina matrix and 0.1-15 wt% zirconium oxide, and the zirconium oxide contains tetragonal phase crystalline zirconium oxide.The Y type molecular sieve catalytic material of the present application has better strength and cracking effect, and the catalyst containing the Y type molecular sieve catalytic material of the present application can improve the selectivity and yield of catalytic cracking gasoline.

The application provides a preparation method of a composite molecular sieve and application of the composite molecular sieve in heavy oil cracking, and the preparation method comprises the following steps: dissolving an aluminum source, a silicon source and a structure directing agent in water, and then performing crystallization treatment to obtain a ZSM-5 crystal seed solution; etching Y type molecular sieve in water by using an alkaline substance to form a hollow structure, and then mixing the hollow Y type molecular sieve with acidic silica sol to obtain a solution containing the hollow Y type molecular sieve; mixing the ZSM-5 crystal seed solution and the solution containing the hollow Y type molecular sieve, and then performing temperature crystallization, and then separating a crystallization product, and then performing washing, drying and calcination to obtain a ZSM-5 / Y composite molecular sieve, and then performing ion exchange reaction, and then performing calcination to obtain a H type ZSM-5 / Y composite molecular sieve product. The composite molecular sieve synthesized by the application has the advantages of high activity, good selectivity and the like when the composite molecular sieve is prepared into a catalyst, high liquefied gas and propylene yield can be obtained, and the composite molecular sieve is particularly suitable for the field of petrochemical catalytic cracking.

A non-oxidative conversion process includes processing a light hydrocarbon feed stream comprising C1 to C3 alkanes in a reactor under catalytic cracking conditions including a temperature of about 850° C. and up to 1020° C. and a residence time of from about 1 second to about 15 seconds in the presence of a catalytic cracking catalyst, thereby producing a product effluent stream comprising a C2 to C10 hydrocarbon product and hydrogen. The product effluent stream contains less than or equal to about 6.5 wt. % of acetylene.

The present application relates to the field of oil refining catalysts, in particular to a catalytic cracking composition, a preparation method thereof, a catalytic cracking aid and application. The catalytic cracking composition comprises a catalytic cracking aid and a catalytic cracking catalyst; the aid comprises, based on the dry basis weight, 10-50 wt% of clay, 40-80 wt% of silicon species in terms of SiO2, 5-30 wt% of aluminum species in terms of Al2O3, 0.5-5 wt% of stable elements in terms of oxides and 0.5-10 wt% of active adjustment elements in terms of oxides; the SiO2 / Al2O3 molar ratio of the silicon species and the aluminum species is 3-30; the specific surface area retention degree of the aid before and after 100% steam treatment at 800 DEG C for 17h is not less than 65%. The catalytic cracking composition is applied to a heavy oil catalytic cracking process, effectively promotes heavy oil conversion, increases the selectivity of high value-added products, reduces the coke yield, and has a high gasoline octane number.

The present application relates to a kind of low sulfur high performance fuel oil production device, it relates to fuel oil production technical field.Low sulfur modified residual oil, hydrogenation low sulfur raffinate are used as main raw material, auxiliary agent A, auxiliary agent B prepared by special oil device are matched, reaction conditions are accurately controlled through DCS system, low sulfur high performance marine fuel oil is prepared in low temperature mild environment;Device integrates vacuum deep pull and viscosity reduction cracking combined process, light fraction can be deep-processed into three kinds of base oil, etc.Additional value products, heavy fraction is reduced in viscosity by viscosity reduction cracking, and low-temperature fluidity is improved;Auxiliary agent B is prepared by dithiophosphoric acid, molybdenum trioxide, epoxy succinic acid polymer, 2,6-naphthalene dicarboxylic acid, anhydrous toluene, phosphorous acid;Fuel oil prepared by the present application, sulfur content is lower, environmental protection is better, low-temperature fluidity is improved, and combustion efficiency is better.

The present invention provides a catalytic cracking catalyst that exhibits high activity even when containing carbon. [Solution] A catalytic cracking catalyst according to one aspect of the present invention contains zeolite and carbon. The zeolite contains hydrogen atoms, oxygen atoms, aluminum atoms, and silicon atoms, as well as atoms of one or more elements selected from alkali metal elements, alkaline earth metal elements, and transition metal elements, in a specific proportion. The weight loss of the catalytic cracking catalyst in thermogravimetric analysis is 0.01 to 1.5% by weight, based on the weight of the catalytic cracking catalyst.

Processes and systems for producing olefins from a crude oil include a steam cracking furnace having a radiant heating section and a convective heating section. One or more heating coils are disposed in the convective heating section for heating a heat transfer fluid. A first heat exchanger heats the crude oil with the heated heat transfer fluid, and the heated crude oil is desalted to form a desalted crude. A second heat exchanger heats the desalted crude with the heated heat transfer fluid to form a preheated desalted crude, which is separated in a first separator to recover a hydrocarbon vapor fraction and a hydrocarbon liquid fraction. A heating coil in the convective section superheats the hydrocarbon vapor fraction and a radiant heating coil in the radiant heating section thermally cracks the superheated vapor fraction to recover a first cracked effluent comprising olefins.

The application discloses a short-time crystallization preparation method of high-crystallinity low-silicon-aluminum ratio H-ZSM-5 molecular sieve and application thereof, and belongs to the field of molecular sieve synthesis. The preparation method comprises the following steps: S1, mixing a silicon source with water to obtain solution A; mixing an aluminum source with water to obtain solution B; mixing an organic amine with water to obtain solution C; S2, adding solution B into solution A, then adding solution C, finally adding seeds, stirring, crystallizing, separating, ion exchanging, drying and roasting to obtain the high-crystallinity low-silicon-aluminum ratio HZSM-5 molecular sieve. The crystallization time is 2-4 h. The HZSM-5 molecular sieve has high crystallinity, the silicon-aluminum ratio is 30-55, the raw material price is low, the amount of organic template agent is small, the synthesis time is very short, the yield is high, the product morphology is hexagonal plate, the particle size is about 2-4 µm, and the HZSM-5 molecular sieve has a good application prospect in the fields of petroleum catalytic cracking and fine chemical industry.

This invention relates to the field of catalysts and discloses a catalyst for methanol cracking to produce hydrogen or methanol reforming to produce hydrogen. The catalyst comprises an active component, an additive, and a support. The active component is copper, and the support is silica. The additive includes any one of nickel, zirconium, cobalt, and zinc. Based on the mass of the catalyst, the content of the active component is 25%-55 wt%, the content of the additive is 1 wt%-7 wt%, and the content of the support is 44 wt%-68 wt%. When used for methanol cracking to produce hydrogen and methanol reforming to produce hydrogen, the catalyst achieves methanol conversion rates of up to 99.8% and 100%, respectively, and H2 selectivity of up to 99.5% and 99.2%, respectively. Furthermore, the catalyst retains high catalytic activity after 220 hours of operation.

This invention belongs to the field of oil refining and chemical engineering, and discloses a saturated light hydrocarbon recovery and purification system and method. The method includes: recovering mercaptan-containing product gas from refinery process feedstock treated with MDEA using an absorption-desorption method; optionally, the method further includes removing mercaptan from the mercaptan-containing product gas; the mercaptan-containing product gas is mercaptan-containing C2 enrichment gas and / or mercaptan-containing crude liquefied petroleum gas; the refinery process feedstock includes refinery rich gas feed and crude hydrocarbon feed. When recovering C2 as a feedstock for ethylene cracking, this invention can remove only hydrogen sulfide and carbon dioxide from the recovered product without removing mercaptan, thus meeting the purity and mercaptan content requirements of the recovered product, reducing repeated desulfurization and sulfur injection processes in the ethylene cracking process, and lowering investment and energy consumption.

This invention provides a catalytic diesel hydrocracking catalyst, its preparation method, and its application. The catalytic diesel hydrocracking catalyst comprises the following components: aluminum-rich ZSM-5 zeolite, a hydrogenation functional component, an optional metal functional modifier, and a binder; wherein the aluminum-rich ZSM-5 zeolite has a silica-alumina molecular ratio between 5 and 15, and the zeolite particles have an average length of less than 20 nm in at least one dimension; the hydrogenation functional component is a sulfide-state metal component. This catalyst, when used in the hydrocracking reaction of catalytic diesel, exhibits advantages such as high selectivity and purity for light aromatics.

This invention provides a process for preparing light white oil with low aromatic content from Fischer-Tropsch synthetic wax, comprising: Fischer-Tropsch synthetic wax undergoing hydrodeoxygenation under hydrorefining conditions to obtain refined Fischer-Tropsch synthetic wax; the refined Fischer-Tropsch synthetic wax entering a hydrocracking reactor undergoing hydrocracking isomerization to obtain wax conversion oil; the wax conversion oil entering a distillation separator undergoing distillation and being cut into diesel fraction and cracking tail oil, the diesel fraction being cut into light white oil, No. 5 industrial white oil, and a 230-290℃ distillate oil; some or all of the cracking tail oil being recycled to the hydrocracking reactor; the refined Fischer-Tropsch synthetic wax passing through a hydrocracking catalyst bed in the hydrocracking reactor, with a refining agent layer at the bottom of the reactor, and refining agent layers above the third and fourth hydrocracking catalyst beds, and quench hydrogen being added above the refining agent layers. This invention reduces the aromatic content in light white oil, achieving the goal of producing high-quality light white oil.

The application discloses a hydroisomerization catalyst and a method for processing Fischer-Tropsch synthesis soft wax into lubricating base oil. The hydroisomerization catalyst is a combined catalyst, comprising catalyst A and catalyst B; wherein the catalyst A is a platinum and / or palladium loaded molecular sieve with a TON structure, and the catalyst B is a platinum and / or palladium loaded molecular sieve with a *MRE structure. The catalyst is used for processing Fischer-Tropsch synthesis soft wax into lubricating base oil. After vacuum distillation of a Fischer-Tropsch synthesis soft wax raw material, a fraction with a distillation temperature greater than 550 DEG C is removed by evaporation, and a fraction with a distillation temperature less than or equal to 550 DEG C is introduced into a hydroisomerization reaction zone. Hydroisomerization and moderate cracking of the soft wax are completed on the hydroisomerization catalyst based on the combined TON structure and *MRE structure molecular sieve shape channel and specific catalytic performance, and a hydroisomerization cracking oil is obtained. The obtained hydroisomerization cracking oil can be processed into low pour point and high viscosity index lubricating base oil by a supplemental refining-fractionation process with a high yield.

The application discloses a method for preparing high-quality cracking material, which comprises the following steps: contacting C5 alkanes and hydrogen with a catalyst in a reactor, and reacting to obtain high-quality cracking material; the C5 alkanes are at least one selected from normal pentane and isopentane; the high-quality cracking material is at least one selected from ethane, propane, normal butane and normal pentane; the catalyst is composed of an acidic carrier and a noble metal active element and an auxiliary element supported on the surface of the acidic carrier; the noble metal active element is at least one selected from palladium and platinum; the auxiliary element is at least one selected from potassium and iron; in the catalyst, the mass ratio of the noble metal active element to the acidic carrier is 0.0001-0.005:1, and the mass ratio of the auxiliary element to the acidic carrier is 0.002-0.05:1.

The application discloses a method for cracking tar into high value-added products, which adopts a route of separating light components by fractional distillation and then hydrogenating heavy components, so that the yield of target products can be affected by hydrogenation of naphthalene, methyl naphthalene and the like below 250 DEG C in the process of hydrocracking, and on the other hand, the components below 250 DEG C account for about 30% to 50%, so that the hydrogen consumption in the subsequent hydrocracking can be reduced by separating the components in advance. After the heavy fraction is subjected to hydrocracking, part of polycyclic aromatic hydrocarbons in the heavy fraction can be cracked into part of monocyclic aromatic hydrocarbons, which can be used for producing aromatic solvent oil, so that the light fraction in the hydrocracking product is separated and mixed into the light fraction generated by pre-fractionation, and the next step processing is carried out, so that the yield of high value-added products can be further improved.

This invention discloses a liquefied petroleum gas (LPG) hydrotreating process for olefin removal and desulfurization. The feedstock consists of one or more types of LPG derived from refinery catalytic cracking, coking, or other units, as well as light hydrocarbons derived from oil and gas fields. After removing hydrogen sulfide from the LPG in a desulfurization tower, the feedstock is pressurized by a feed pump, mixed with hydrogen, and then heated and vaporized in a heat exchanger and furnace. It then enters a hydrorefining reactor for olefin saturation, removal of mercaptans and other impurities, and then enters a desulfurization reactor to remove hydrogen sulfide generated during the hydrotreating reaction. The refined desulfurized LPG is then cooled by heat exchange and enters a low-pressure separator. The refined LPG after gas-liquid separation is sent to a LPG separation unit. This process yields refined LPG products with low olefin and low sulfur content.

The application discloses a catalyst for preparing ethylene and propylene through catalytic cracking, and the catalyst comprises silicon dioxide, potassium, a molecular sieve and a metal or an oxide thereof attached to the molecular sieve, and the mass ratio of the molecular sieve, the silicon dioxide, the metal oxide and K2O is 30-50:30-65:5-20:0.1-5, and the metal is calculated according to its metal oxide when the catalyst comprises the metal; the potassium in the catalyst is calculated according to potassium oxide. The application further discloses preparation and application of the catalyst. The ZSM-5 molecular sieve modified by the double metal and containing potassium salt is used as the catalyst, the activity of the catalyst is improved, the conversion rate of n-butane is greatly improved, and the ethylene and propylene yield is improved.

The application discloses a Beta / ZSM-5 symbiotic zeolite molecular sieve, a hydrocracking catalyst and a preparation method and application thereof. The Beta / ZSM-5 symbiotic zeolite molecular sieve has the topological structures of BEA and MFI, wherein the particle size of the particle with the topological structure of BEA is 50-500 nm, and the particle size of the particle with the topological structure of MFI is 3-6 mu m; preferably, the molar ratio of the silicon-aluminum oxide molecular substance of the Beta / ZSM-5 symbiotic zeolite molecular sieve is 25-300, preferably 50-200. The hydrocracking catalyst is applied to a catalytic diesel hydrocracking reaction, and the yield of light aromatic hydrocarbons and benzene in the reaction product can be effectively improved.

The application aims to provide a method for loading zinc atom clusters on the surface of ruthenium nanoparticles by breaking Zn-N bonds based on H2 thermal drive and application, and belongs to the technical field of preparation of nanometer catalytic materials; the method takes a double-limiting material containing coordination limited Zn-N4 and narrow hole limited Ru clusters as a precursor, thereby ensuring uniform dispersion and close proximity of initial active sites; H2 is used as a key inducer, active hydrogen species generated by catalytic cracking of hydrogen by ruthenium sites is used, and hydrogen overflow effect is used to realize the breaking of thermodynamically stable Zn-N bonds; high-mobility Zn atoms are obtained and finally selectively captured on the surface of Ru nanoparticles; Zn species diffuse, nucleate and grow on the surface of Ru crystals to form sub-nanometer scale Zn atom clusters through self-assembly; and the material can improve the intrinsic catalytic activity and stability of Ru-based catalysts and provide a new way for efficient energy conversion.

This invention belongs to the field of hydrogen production technology and discloses a natural gas catalyst cracking hydrogen production process. The system is equipped with a closed-loop circulation transfer system and a non-stop online replacement mechanism. In key stages such as catalyst deactivation and carbon deposit product collection, the overall production process can be completed without stopping the process. The deactivated catalyst can be replaced in a sealed manner, new catalyst can be loaded, and the reaction tank can be reset quickly. Based on the intelligent scheduling algorithm, the transfer path is dynamically optimized. With the flexible sealing docking structure, the process of each station can be seamlessly connected. Furthermore, the core reaction conditions such as feed, temperature, and pressure are stabilized through a multi-parameter collaborative control algorithm to ensure that the cracking conversion efficiency is continuously and stably up to standard, thereby improving the system's capacity utilization and overall production efficiency. The system adopts a three-level interlock self-inspection mechanism to complete the special inspection of all nodes of communication, equipment, sensors, valves, and interlock logic. If any link is abnormal, the entire system will be immediately triggered to stop the interlock and terminate the subsequent processes.

The application discloses a method for producing propylene by ethylene methylation, and belongs to the technical field of propylene preparation. The method provided by the application comprises the following steps: reacting a mixture containing raw gas and a catalyst to obtain propylene; the raw gas comprises ethylene and a methylation reagent; and the catalyst comprises an acidic BIK molecular sieve and / or a modified MOR molecular sieve. The method has the advantages of high propylene selectivity, good catalyst stability, mild reaction conditions, simple process and the like, and can be applied to adjusting the olefin product structure of a methanol-to-olefins (MTO) process, a fluidized catalytic cracking (FCC) process and the like, and has a wide application prospect.

This invention discloses a catalyst for the production of ethylene and propylene, its preparation method, and its applications. The catalyst comprises the following components: I) 1%–10% of chemical formula A x B y D z A compound of O4; in the chemical formula, the oxidation states of elements A, B, and D are m, n, and p, respectively, satisfying x·m + y·n + z·p = 8, where m, n, and p are integers not greater than 3; the A x B y D z O4 has a spinel structure; II) 0.5%–10% is selected from at least one oxide of rare earth elements, P, Mo, and W; III) 20.0%–55.0% is selected from at least one zeolite of ZSM-5 and ZSM-11; IV) 10%–30% is a binder; V) 25.0%–60.0% is clay. This catalyst is used in the catalytic cracking of petroleum hydrocarbons to produce ethylene and propylene, and features good catalyst stability, low methane yield, and high ethylene and propylene yields.

The application discloses a kind of production low freezing diesel oil hydrogenation cracking method.The method includes hydrogenation refining reactor and hydrogenation cracking reactor arranged in series, wherein hydrogenation cracking reactor is provided with hydrogenation cracking catalyst bed and post hydrogenation refining catalyst bed, and the method is as follows: wax oil raw material and hydrogen enter hydrogenation refining reactor, contact with hydrogenation refining catalyst to carry out hydrogenation refining reaction, and obtain hydrogenation refining stream;Hydrogenation refining stream enters hydrogenation cracking reactor, material P is introduced into hydrogenation cracking reactor between hydrogenation cracking catalyst bed and post hydrogenation refining catalyst bed, and the product obtained in hydrogenation cracking reactor enters air cooling device, wherein air cooling device is water injected, so that material P in product is carried out by water phase and leaves reaction system, and after air cooling, oil phase product is separated and fractionated, and diesel oil fraction is obtained.The method of the application can improve the quality of low freezing diesel oil while improving the yield of low freezing diesel oil in hydrogenation cracking device.

This invention discloses an oleic acid oxidative cracking catalyst, its preparation method, and its application, belonging to the field of catalyst preparation technology. The catalyst for the oxidative cracking of oleic acid to azelaic acid is prepared by: uniformly mixing phosphotungstic acid with an organic onium salt, and then ball milling the mixture in a ball mill jar. The preparation method is simple, generates no waste, and produces a catalyst with high yield and high activity. In the process of oleic acid cracking to azelaic acid, the conversion rate of oleic acid reaches 100%, and the selectivity of azelaic acid reaches 96%.

Methods for processing a crude oil feedstock include introducing a crude oil stream to a reactive distillation unit to remove conradson carbon and metals from the crude oil stream and generate a distillate stream having a mean boiling point distribution less than the crude oil stream and passing the distillate stream in a gaseous form in a continuous manner and without further processing to a catalytic cracking reactor that cracks the distillate stream to form a petrochemical product stream including light olefins and BTX. The catalytic cracking reactor includes a cracking catalyst and a susceptor material dispersed throughout the catalytic cracking reactor. Further, the catalytic cracking reactor operates at a temperature of 300° C. to 800° C. with heating from magnetic induction of the susceptor material.

A process for producing monomers is disclosed. The process comprises hydrocracking a pyrolysis oil stream in a hydrocracking reactor over a hydrocracking catalyst in the presence of a hydrocracking hydrogen stream at hydrocracking conditions to open rings present in said pyrolysis oil stream to produce a hydrocracked effluent stream. The hydrocracked effluent stream is fractionating in a fractionation column to provide a naphtha stream. The naphtha stream is contacted with a NEP catalyst and hydrogen to produce a light paraffinic stream or with a reforming catalyst to produce an aromatics stream.

This invention discloses a liquefied petroleum gas (LPG) hydrodeolefins desulfurization process. The raw materials are one or more types of LPG derived from refinery catalytic cracking, coking, and other units, as well as light hydrocarbons derived from oil and gas fields. The incoming LPG is pressurized and mixed with hydrogen, then heated and vaporized before entering the hydrorefining reactor. The high-temperature gaseous hydrorefining reaction product enters the desulfurization reactor for fine desulfurization. The reaction effluent after fine desulfurization is heat-exchanged and cooled before entering a low-pressure separator. The low-pressure separator generates a low-density gas at the top, which is pressurized and mixed with fresh hydrogen from outside the unit to form mixed hydrogen. The refined LPG at the bottom of the low-pressure separator is pressurized and sent to the gas separation unit.