123 results about "Space velocity" patented technology

The invention relates to the technical field of methane cracking and hydrogen production, and discloses a metal-modified Co-Bi liquid alloy catalyst, wherein the catalyst uses Co as an active component, uses Bi low melting point metal as a solvent, and uses a third metal M as an auxiliary agent; the invention also discloses a method for preparing the catalyst, comprising: calcining a cobalt salt to generate cobalt oxide, and then forming CoO-MO X The mixture powder was finally heated under N2 and H2 atmosphere to obtain CoO‑MO X The powder is mixed with elemental Bi to obtain a cobalt-bismuth ternary liquid alloy catalyst; the present invention also discloses a method for applying the catalyst to methane cracking and hydrogen production, comprising: heating the preheating furnace to a certain temperature, introducing pure methane gas, and reacting under normal pressure, at a temperature of 500 to 700°C, with a methane space velocity of 1 to 100 mL / g·min, and after the reaction is completed, the temperature drops to room temperature in an N2 atmosphere, and the carbon product is taken out of the reaction tube after cooling. The catalyst disclosed by the present invention has the advantages of high activity, good stability, strong methane cracking ability, mild reaction conditions, simple preparation process, and long life.

The invention discloses a catalytic method for converting alpha-olefin in an alkane-olefin mixture into internal olefin and application, raw materials and a solid acid catalyst are carried out in a fixed bed or a reaction kettle, the reaction temperature is 50-150 DEG C, the reaction pressure is 15-400 psi, and the reaction environment is an inert gas atmosphere; when the reaction is carried out on the fixed bed, the mass space velocity of the solid acid catalyst is 1h <-1 >-20h <-1 >; when the reaction is carried out in the reaction kettle, the conversion frequency of the raw materials is 5000 mol substrate mol acid site density <-1 > h <-1 > to 50000 mol substrate mol acid site density <-1 > h <-1 >; wherein the raw material is an alkane-alkene mixture; the solid acid catalyst comprises an active component and a carrier, wherein the carrier contains at least one inorganic oxide; the active component has a structure as shown in a formula (1) and / or a formula (2), in the formula (1) and the formula (2), R is alkyl or phenyl, and n is greater than or equal to 1. According to the catalysis method provided by the invention, the conversion rate of alpha-olefin can be increased, and the proportion of skeleton isomerization products and oligomers in internal olefin products can be reduced.

The invention provides a Ru / MgO-La2O3 catalyst for efficiently catalyzing ammonia decomposition to produce hydrogen as well as a preparation method and application of the Ru / MgO-La2O3 catalyst, and belongs to the technical field of ammonia decomposition to produce hydrogen. The catalyst is prepared by taking noble metal Ru as an active component and MgO-La2O3 composite oxide as a carrier through a coprecipitation method and an impregnation method. The loading capacity of Ru in the catalyst is 1-20 wt%, and the dispersity and ammonia decomposition reaction activity of Ru are remarkably improved by optimizing the interaction between the carrier and the metal-carrier. The preparation method comprises the following steps: mixing a ruthenium precursor with the MgO-La2O3 carrier, and carrying out drying, calcining and reduction treatment to obtain the high-dispersion Ru / MgO-La2O3 catalyst. Compared with the existing noble metal-based catalyst, the composite carrier regulates and controls the electronic structure of Ru, so that the composite carrier shows excellent ammonia decomposition activity and stability at low temperature (350-550 DEG C), the ammonia conversion rate at 450 DEG C can reach 99.5%, and efficient total conversion is still kept under the conditions of high temperature and high space velocity. The Ru / MgO-La2O3 catalyst obtained by the method is superior to most reported catalysts under the same condition, the catalyst preparation process is simple, the cost is controllable, the method is suitable for large-scale production, and an efficient and economical technical scheme is provided for the field of hydrogen energy storage and transportation.

A process method for preparing acrylonitrile through propylene ammoxidation belongs to the field of chemical engineering, and is characterized in that in a corresponding device and a reaction system of the method, propylene, ammonia gas and air (in terms of O2) enter a fluidized bed reactor at 400-450 DEG C and 0.01-0.15 MPa for reaction according to a ratio of 1: (1-1.5): (2-10) at a weight hourly space velocity of 0.04-0.1 h <-1 >; the micro-sphere catalyst with the particle size of 40-60 microns in the dense-phase section and the dilute-phase section has alpha-phase bismuth molybdate, gamma-phase bismuth molybdate and lattice oxygen active centers and meets the chemical formula MoaBibNicWdTleVfPgSixOy, the atomic ratio a in the formula is 21-22, the atomic ratio b in the formula is 1.5-2, the atomic ratio c in the formula is 4-5, the atomic ratio d in the formula is 0.8-1, the atomic ratio e in the formula is 0.09-0.1, the atomic ratio f in the formula is 0.15-0.2, the atomic ratio g in the formula is 0.8-1, the atomic ratio x in the formula is 70-71, and y is the number of oxygen atoms needed by the atomic valence of all elements; a product enters a quench tower and a water absorption tower to be neutralized and cooled, and then passes through a recovery tower, an acetonitrile tower, a decyanation tower, a layering device and a finished product tower to realize separation of a water phase and an organic phase, so that crude acetonitrile, hydrocyanic acid and refined acrylonitrile are further obtained. The process is good in conversion degree and product selectivity, stable and reliable in operation, energy-saving and environment-friendly.

The invention discloses application of a supported heterogeneous catalyst of oxide and copper-manganese spinel in preparation of acetaldehyde by anaerobic dehydrogenation of ethanol, and belongs to the technical field of heterogeneous catalysis for preparation of acetaldehyde and hydrogen by anaerobic dehydrogenation of ethanol. The reaction is carried out in a fixed bed reactor, under the conditions that the reaction atmosphere is nitrogen, the reaction temperature is 280 DEG C and the mass space velocity is 66.1 h <-1 >, the ethanol conversion rate is 72.5%, the acetaldehyde selectivity is 95.0%, and the space time yield of acetaldehyde based on the copper-manganese composite oxide is 43.5 h <-1 >, so that high-selectivity preparation of acetaldehyde and hydrogen under relatively mild conditions is realized; the system has the remarkable advantages of simple catalyst preparation, high catalytic activity under the condition of high mass airspeed, high space-time yield of acetaldehyde, high atom utilization rate of the system, good stability and the like. The CuMnTi-1 catalyst can be stabilized for more than 70 hours, the CuMnTi-1 improves the utilization rate of copper and manganese, improves the catalytic performance, reduces the demand quantity of copper-manganese spinel in the reaction, and reduces the overall cost of catalyst preparation.

The invention relates to a non-sulfur-tolerant wide-temperature shift regulation and control process based on a coal natural gas methanation process, and belongs to the technical field of coal chemical industry. The process comprises the following specific steps: carrying out non-sulfur-tolerant wide-temperature shift reaction on purified raw materials for methanation reaction, namely carrying out adiabatic and / or isothermal CO shift reaction under the conditions that the temperature is 200-360 DEG C, the pressure is 1-10 MPa, the molar ratio of H2O to CO is 0.7-2 and the air speed is 3000-40000h <-1 >, reducing the CO concentration at the inlet of a methanation reactor by 30-70%, and then carrying out high-temperature reaction on the methanation reaction to obtain the high-sulfur-tolerant methanation reaction. The CO disproportionation reaction in the methanation reactor is avoided while the circulating gas is effectively reduced, the service life of the existing methanation catalyst is prolonged by more than 50%, and the shutdown frequency and the maintenance time are greatly reduced.

This invention discloses a low-space-velocity (SCR) catalyst and its preparation method. The catalyst includes a coating and a support layer. The coating comprises a coating material consisting of a mixture of tungsten-doped (5%) anatase nano-titanium dioxide, titanium dioxide, and SSZ-13 molecular sieve, with a content of 56.1 wt% to 75.6 wt% of the total loading. The method includes the following steps: preparing a support layer solution and a coating material; preparing a catalyst slurry; drying a catalyst support with a support layer solution; coating the catalyst support with the catalyst slurry; and calcining and drying to obtain the catalyst. This invention improves the coating uniformity and efficiency by coating the support layer solution and the catalyst slurry, thereby improving the NO content of the catalyst under low space velocity conditions. x Conversion efficiency.

The invention relates to a method of producing at least one alkene from at least one ketone, the method comprising the step of: (a) contacting at least one gaseous ketone with at least one ketonization catalyst in the presence of at least one hydrogen releasing agent or hydrogen at a temperature of at least 350°C to produce a corresponding alkene, wherein the gases have a gas hourly space velocity (GHSV) of 1 to 1000 m 3 / (m 3 x h), and wherein the ketonization catalyst is a metal oxide catalyst or mixtures thereof.

The invention provides a reaction system for preparing aromatic hydrocarbon through hydrogenation of carbon dioxide. The reaction system comprises an injection loop reactor, a rectification device and a recycle gas separation device, the injection loop reactor comprises a reaction kettle, a circulating pump, a reaction heat exchanger, a cross-flow filter and a Venturi injector which are communicated in sequence; part of the Venturi ejector is arranged in the reaction kettle, and the circulating gas separation device comprises a primary condenser, a secondary condenser, an absorption tower and a desorption tower which are communicated in sequence; the device further comprises a circulating gas heater. The jet loop reactor is adopted as key process equipment to perform carbon dioxide hydrogenation reaction to continuously prepare aromatic hydrocarbon, reaction fluid circulates in a loop in a large flow manner and is jetted at a high speed by the Venturi jet, and negative pressure is formed at a working nozzle, so that process gas is sucked into the jet to form micron-sized bubbles with large specific surface area, and the aromatic hydrocarbon is continuously prepared. Gas-liquid-solid contact is increased, the gas-liquid-solid multi-phase reaction speed can be increased, the reaction efficiency is improved, and therefore the air speed is increased under the condition that the yield is guaranteed.

The invention belongs to the technical field of CO2 catalytic conversion, and discloses an in-situ reduction efficient CO2 methanation catalyst as well as a preparation method and application thereof. The efficient CO2 methanation catalyst NiA (CO3) xRe is formed by in-situ reduction of Ni and A coupled carbonate NiA (CO3) x, wherein A is selected from one of Mg, Ce and Al. NiA (CO3) xRe is prepared by a coprecipitation method. According to the present invention, the reaction equilibrium conversion is achieved at 300 DEG C in the reaction atmosphere with the CO2: H2: N2 volume ratio of 1: 4: 5 and the air speed of 150000 mL.gcat <-1 >. H <-1 >, the methane selectivity reaches 100%, the methane yield reaches 677.8 mmol.gcat <-1 >. H <-1 >, and the methane selectivity is still not reduced after the operation is performed for 100 h under the condition; compared with the prior art, the prepared catalyst greatly improves the high efficiency and stability of methanation catalytic reaction, the preparation process is simple, large-scale production is easy to achieve, the catalyst is matched with the temperature of coal-fired flue gas, energy does not need to be input again, efficient conversion can be completed, carbon emission is effectively reduced, and high-value products are obtained for use; and a favorable way is provided for realizing a carbon neutralization target.

A reactor system and method for the catalytic dehydrogenation of saturated C3-C6 hydrocarbons within a reactor placed within a reactor settler, where the reactor is open at its bottom and open to the settler, and the outlet riser of the reactor is not rigidly coupled to at least one downstream cyclone. This configuration allows the amount of catalyst within the reactor to be controlled by varying the catalyst level in a reactor settler external to the reactor, and allows the total catalyst retention amount and / or weight hourly space velocity (WHSV) to be controlled independently of the catalyst flow from the catalyst regenerator.

A catalytic cracking process for producing light olefins and aromatic gasoline includes contacting a petroleum-based feedstock with a catalyst in a single riser reactor, where the catalyst includes 0 wt % to about 15 wt % of a Y-type zeolite and greater than 30 wt % of a pentasil zeolite, a weight ratio of pentasil zeolite to Y-type zeolite greater than 3; and a weight hourly space velocity (WHSV) is about 40 h−1 to about 120 h−1.

The invention first relates to a process for the dehydrogenation of a feedstock comprising cycloalkanes having 6 carbon rings to produce an effluent comprising hydrogen and aromatics, using a reaction section comprising at least one multi-tubular reactor comprising at least two tubes comprising a fixed bed of at least one dehydrogenation catalyst and a shell comprising at least one fixed bed of at least one dehydrogenation catalyst, -the feedstock is fed into the tube in gaseous form at an inlet temperature of the feedstock greater than or equal to 300 DEG C, at an inlet pressure of the feedstock between 0.1 and 1 MPa, and at a feedstock weight hourly space velocity (WWH) at an inlet between 1 and 15 h <-1 >,-a heat transfer fluid is circulated in the shell, the heat transfer fluid is introduced in gaseous form at the inlet of the shell, and-the heat transfer fluid is introduced in gaseous form at the inlet of the shell. The heat transfer fluid is introduced into the shell at an inlet temperature of between 320 DEG C and 400 DEG C and at an inlet pressure of between 0.10 MPa and 1.10 MPa at a flow rate such that the ratio of the weight flow rate of the heat transfer fluid at the inlet of the shell to the weight flow rate of the feedstock at the inlet of the tube is greater than or equal to 1.0.

The invention relates to the technical field of diene hydrogenation preparation, in particular to a preparation method of exo-tetrahydrodicyclopentadiene, which comprises the following steps of: performing catalytic hydrogenation on a dicyclopentadiene solution by using a circulating continuous flow bubbling hydrogenation reactor at the normal pressure and the temperature of 70-90 DEG C at the volume space velocity of 5h <-1 > and the hydrogen-oil volume ratio of 750-850 to obtain exo-tetrahydrodicyclopentadiene, automatically separating the hydrogenation catalyst at the tail end of the reactor to obtain a hydrogenation product, stirring and mixing an isomerization catalyst and the hydrogenation product at 90-110 DEG C, and carrying out catalytic isomerization to prepare exo-tetrahydrodicyclopentadiene; and rectifying and separating to obtain hanging tetrahydrodicyclopentadiene. According to the invention, the circulating continuous flow bubbling hydrogenation reactor is adopted for liquid phase hydrogenation, continuous production of exo-tetrahydrodicyclopentadiene is realized by a two-step method, the problem that catalytic hydrogenation and isomerization reaction are not matched is avoided, the conversion rate of exo-tetrahydrodicyclopentadiene is increased, and coking and impurity pollution of non-target products are reduced.

A selective hydrogenation method for ethane cracking to olefins involves selectively hydrogenating the ethylene feedstock from the top of an ethane stripper to remove acetylene. Reaction conditions: inlet temperature 50℃~95℃, pressure 1.5~3.0MPa, space velocity 8000~14000h⁻¹ ‑1 The preferred reaction conditions are: reactor inlet temperature 60℃~90℃, reaction pressure 2.0~2.5MPa, and space velocity 9000~12000h⁻¹. ‑1 The catalyst support is alumina or mainly alumina, and has a bimodal pore structure. The specific surface area of ​​the catalyst is 3–16 m². 2 The catalyst contains at least Pd, Fe, Ni, and Cu, with Pd supported in both microemulsion and solution formats. Ni and Cu are supported in microemulsion, while Fe is supported in solution. The solution-supported Pd and Fe are primarily located in the 56–75 nm micropores, while the microemulsion-supported Ni, Cu, and Pd are mainly distributed in the 300–650 nm macropores of the support. This alkyne removal method exhibits excellent catalytic performance and anti-coking properties, with low "green oil" formation.

The application relates to a preparation method of a high-temperature-resistant high-space-velocity VOCs catalytic combustion catalyst for acid ester waste gas and the catalyst, and belongs to the field of industrial waste gas treatment. The catalyst takes noble metal, transition metal oxide and rare earth oxide as active components, takes honeycomb ceramic or metal honeycomb as a carrier, and is prepared by adopting a coating process. First, Ce x Zr 0.6‑x La y Pr 0.1‑ y O2 is prepared by using lanthanum nitrate hexahydrate, praseodymium nitrate hexahydrate, cerium nitrate hexahydrate and zirconium nitrate pentahydrate; then, La-Al2O3 is prepared by using lanthanum nitrate hexahydrate and Al2O3 through an equal-volume impregnation method; and finally, the catalyst is prepared by using Ce x Zr 0.6‑x La y Pr 0.1‑ y O2, La-Al2O3 and noble metal. The catalyst has the characteristics of high low-temperature activity, good thermal stability and high purification efficiency for catalytic combustion of volatile organic compounds of acid esters at high space velocity.

The invention provides a selective hydrogenation method for C1-C3 fractions, the C1-C3 fractions come from the top of a depropanizer of an ethylene device, and the process conditions of the hydrogenation reaction are as follows: the inlet temperature of a reactor is 90-130 DEG C, and the gas volume space velocity is 6000-20000h <-1 >; in the C1-C3 fractions, the content of H2 is 10%-30%, the content of C2H4 is 25%-40%, the content of C2H2 is 0.4%-0.9%, the content of C3H6 is 5%-11%, the content of PDMA is 0.2%-1.2%, the content of CO is 0.03%-0.2%, the content of butadiene is less than or equal to 0.2%, and the balance is methane, ethane and propane. According to the hydrogenation method, non-noble metal Fe is adopted as a catalyst of a main active component, and process parameter control is combined, so that the CO fluctuation resistance of the catalyst is improved, the selective hydrogenation efficiency of C1-C3 fractions is ensured, and meanwhile, the cost of the catalyst is reduced.

The invention relates to a process for converting CO2 into methane, wherein hydrogen is contacted with a gaseous feed comprising CO2 in at least one methanation reactor comprising a catalyst bed at a catalyst bed temperature of 160°C to 550°C at a pressure of 0.1 MPa to 1 MPa, wherein the gas hourly space velocity is 10 m 3 / kg / hour to 50 m 3 / kg / hour, and wherein the H2 / CO2 molar ratio is 1 to 8, and wherein the catalyst comprises Ni metal deposited on a substrate made of uranium oxide having the formula UO 2+x , wherein x is 0.01 to 0.6, and wherein the mass content of nickel is 5% to 40% of nickel metal relative to the total mass of the catalyst.

The invention relates to a process condition simulation method and simulation device for regulating and controlling the burn-out rate of dry quenching. The method comprises the following steps: setting the temperature rise time in a simulation reaction to be equal to the cooling time of coke in a dry quenching furnace in industrial production; the initial temperature is equal to the coke discharge temperature of a dry quenching furnace in industrial production; the volume flow rate of the mixed gas is determined by the volume space velocity of cooled circulating gas reacted with coke in the fixed bed in industrial production and the accumulation volume of a coke material in the simulated reaction; the concentration of reaction gas is equal to that of circulating gas in industrial production; the method comprises the following steps: placing a coke material in a constant-temperature area of a reaction section, heating to an initial temperature, recording the mass, then introducing a mixed gas of a reaction gas and an inert gas, heating to a red coke temperature from the initial temperature within the heating time, and recording the mass; and calculating the dry quenching burn-out rate. Compared with the prior art, the method provided by the invention has the advantages that the integrating degree of conditions and actual working conditions is high, and the influence of the actual working condition change on the dry quenching burn-out rate can be accurately reflected.

The utility model provides an external heat extraction alkylation capacity expansion system which comprises a feeding pipe, a first heat exchanger, a second heat exchanger, an alkylation reactor, a first compressor, a third heat exchanger, a refrigerant water tank and a refrigerating unit, the feeding pipe sequentially passes through the first heat exchanger and the second heat exchanger, and the second heat exchanger is connected with the inlet end of the alkylation reactor; the outlet end of the alkylation reactor is connected with the first compressor; the second heat exchanger is further connected with a third heat exchanger through a bypass, the third heat exchanger, the refrigerant water tank and the refrigerating unit are sequentially connected to form a circulating water path, a circulating pump is arranged on the circulating water path, and the third heat exchanger is connected with the inlet end of the alkylation reactor. According to the alkylation reactor, the device capacity expansion can be better realized in the allowable range of the airspeed of the reactor by reducing the raw material feeding temperature and the reaction temperature, meanwhile, the refrigeration load can be flexibly adjusted according to the feeding temperature of the alkylation reactor, and the shutdown time is short and the equipment transformation cost is low when the equipment is upgraded.

This invention belongs to the field of chemical product synthesis technology and discloses a method for isomerization of methylphenolic compounds. Under certain reaction temperature and pressure conditions, methylphenolic compounds are vaporized and mixed with a carrier gas. The mixture passes through a fixed-bed reactor containing a bilayer modified ZSM-5 catalyst at a certain space velocity, where it undergoes an isomerization reaction to generate its isomer products. The ZSM-5 catalyst contains Si, Al, Fe, and Ge elements. This invention, by introducing metal heteroatom components into the ZSM-5 molecular sieve framework, effectively improves the pore structure and active sites of the molecular sieve, enhances the catalyst's resistance to carbon deposition, strengthens its activity and stability, and significantly extends its lifespan. Furthermore, it exhibits excellent catalytic effects on the isomerization of various methylphenolic compounds.

The application provides a low-temperature high-activity supported Ru-based catalyst, a preparation method and application, the method is characterized in that a manganese oxide carrier is synthesized by a precipitation method, the manganese oxide carrier is loaded by a deposition precipitation method, and a supported Ru-based catalyst is obtained. ‑1 ·h ‑1 Under high space velocity conditions, a CO2 conversion rate of 94.9% and a selectivity of 100% are achieved, the bottleneck of insufficient low-temperature activity of existing catalysts is broken through; meanwhile, the catalyst exhibits excellent long-term stability, after continuous operation for 100 hours at 180 DEG C, the CO2 conversion rate attenuation is less than 0.5%, and the selectivity is always kept at 100%, laying a solid durability foundation for industrial application.

The present invention relates to a process for preparing and processing of synthesis gas, the process particularly comprising the steps of preparing a first gas stream comprises H2 and CO2; feeding said gas stream into a first reactor comprising a reverse water gas shift catalyst, wherein said gas stream is fed into the first reactor at a gas hourly space velocity (GHSV) in the range of from 1,000 to 100,000 h-1, wherein the reverse water gas shift reaction is conducted at a temperature in the range of from 650 to 1,000 °C, wherein in a time interval Δt, wherein Δt is in the range of from 1 to 60 minutes, the GHSV of said gas stream displays a gradient in the range of from 2,000 to 60,000 h-1, obtaining a second gas stream; feeding the second gas stream into a second reactor, wherein the second reactor comprises one or more of a methanol synthesis catalyst, a dimethyl ether synthesis catalyst, an oxo synthesis or hydroformylation catalyst, a Fischer-Tropsch synthesis catalyst, a formic acid synthesis catalyst, and a phosgene synthesis catalyst, obtaining a product stream.

The present invention relates to a process and an apparatus for hydrotreating a liquid oil stream, such as a pyrolysis oil stream, by continuously operating in a fixed bed reactor, in the presence of a reduced nickel (Ni) catalyst, the liquid oil stream is reacted with hydrogen at a temperature of 80-250 DEG C, a pressure of 10-200 barg, a liquid hourly space velocity (LHSV) of 0.1-6.0 h <-1 >, and a hydrogen / liquid oil ratio (defined as the volume ratio of hydrogen to liquid oil stream flow) of 100-8000 NL / L to form a stabilized liquid oil stream.

The invention discloses a method for preparing a carbon nano tube through H2 in-situ regulation and control of a Ni-CeO2 / Al2O3 nano island catalytic material, and relates to the field of chemical catalysis. The reaction is carried out in a vertical quartz tube of a high-temperature furnace of the fixed bed reactor, the catalyst is Ni-CeO2 / Al2O3-X with nano island morphology and is fixed on the upper section, and the lower section is connected with a detachable collection bottle; the volume ratio of raw material gas CH4 to CO2 is 1: 1, the reaction is carried out under the conditions that the temperature is 750 DEG C, the pressure is normal and the mass space velocity is 160000 mL gcat-h, and the carbon nano tube and the synthesis gas are co-produced. According to the process, three synchronization of high yield of CNTs, stable yield of synthesis gas and long service life of the catalyst is realized for the first time, and a low-cost, green and scalable industrial route is provided for large-scale preparation of high-purity carbon nanotubes from CO2-CH4.

The present invention is a method for producing a catalyst-free olefin by continuous operation in a fixed-bed reactor at a temperature of 80 to 250°C, a total pressure of 10 to 200 barg, and a liquid hourly space velocity (LHSV) of 0.1 to 6 h -1 and a method for hydrotreating a nitrogen-enriched liquid oil stream by reacting said nitrogen-enriched liquid oil stream with hydrogen, thereby producing a stabilized liquid oil stream.

The invention relates to the field of petrochemical engineering, and discloses an efficient catalytic cracking method and system based on a ZMQ-1 molecular sieve, which takes a heavy oil product subjected to desulfurization and metal impurity removal as a raw material, and performs cracking reaction by using a catalyst taking the ZMQ-1 molecular sieve as a core. The reaction conditions are as follows: the temperature is 450-550 DEG C, the pressure is 0.1-0.3 MPa, the weight ratio of the catalyst to the raw materials is 1: 10-1: 20, and the space velocity is 2-6h <-1 >; and low-carbon olefins, light aromatic hydrocarbons and gasoline fractions are recovered from cracking products through gas-liquid separation, and uncracked heavy oil products can be cyclically subjected to secondary cracking. The system comprises a raw material pretreatment unit, a catalytic cracking unit, a product separation unit and an uncracked component reflux unit. According to the present invention, through the grading pore channel design of the ZMQ-1 molecular sieve and the introduction of the appropriate metal auxiliary agent, the efficient conversion of the heavy oil, the selective generation of the target product and the significant reduction of the coke generation amount are achieved, and the characteristics of green low carbon, high efficiency and energy saving are provided.

The invention relates to the technical field of chemical catalysis and separation, in particular to a tungsten (W) doped MFI type molecular sieve membrane (W-MFI) and catalyst integrated membrane reactor which is used for efficiently catalyzing propane dehydrogenation to prepare propylene. The W-doped MFI molecular sieve membrane (W-MFI) is used as a key membrane material of the membrane reactor, so that the overall performance and stability of the membrane reactor are remarkably improved. The introduction of W not only enhances the thermal stability and chemical stability of the molecular sieve membrane and effectively prevents the collapse risk of the membrane structure at high temperature, but also enables the membrane reactor to maintain stable performance output in a 24-hour operation process. And in the aspect of catalytic performance, the prepared membrane reactor has the propane conversion rate of 44% and the propylene selectivity of more than 98% under the conditions that the temperature is 550 DEG C, the mass space velocity is 3.6 h <-1 >, the ratio of C3H8 to N2 is 1: 3 and argon purging is performed (30 mL / min), and compared with a membrane reactor of a pure silicon MFI molecular sieve membrane, the performance is greatly improved.

The invention discloses a method for producing hexafluoropropylene from vinylidene fluoride, which comprises the following steps: mixing VDF and diluent gas (nitrogen / argon) according to a ratio of 1: (3-8), preheating, introducing into a fixed bed reactor filled with a CrO-MnO / gamma-AlO catalyst, reacting under the conditions of 350-450 DEG C, 0.1-0.5 MPa and air speed of 1000-3000h <-1 >, and separating the product to obtain high-purity hexafluoropropylene. Through collaborative optimization of catalyst components and design of a mild reaction system, 88% of VDF conversion rate, 90% of HFP selectivity and 99.8% of product purity are achieved, energy consumption and equipment cost are remarkably reduced, and the method is suitable for industrial continuous production.

The invention discloses a method and a device for preparing maleic anhydride by oxidizing n-butane, and relates to the technical field of maleic anhydride synthesis. According to the method, n-butane and oxygen-containing gas are subjected to catalytic oxidation in a pressurized reactor, and the reaction temperature is reduced and the reaction space velocity is increased, so that the selectivity of generating maleic anhydride through oxidation of n-butane is improved, and the generation of by-products such as carbon monoxide and carbon dioxide is reduced; maleic anhydride rich oil and maleic anhydride tail gas are obtained after maleic anhydride material flow obtained through reaction is cooled and absorbed, the maleic anhydride tail gas is divided into two gas flows to be recycled, one gas flow is pressurized and then serves as raw material gas to be returned to a pressurization reactor for reaction, and the other gas flow enters a conventional reactor for catalytic oxidation; the utilization rate of n-butane and the total conversion rate of the reaction can be obviously improved, and gases such as carbon dioxide and carbon monoxide in the system are not accumulated in the pressurized reaction system; the maleic anhydride and the maleic anhydride tail gas are separated by adopting a two-stage pressurized absorption method, so that the water content in the separated maleic anhydride product is lower than 0.2%.