53 results about "Space velocity" patented technology

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 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 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.

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.

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 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.

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 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 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 application relates to the technical field of 1-butene oligomer preparation, and more particularly to a process for producing 1-butene trimer, i.e., dodecene. The present application provides a process for producing 1-butene trimer, which comprises: subjecting initial raw materials containing butane and 1-butene to catalytic reaction in a fixed-bed tubular reactor under the conditions of 50-100 DEG C, 1-2 MPa pressure, raw material space velocity 0.5-2 h ‑1 -1 of the fixed-bed tubular reactor containing a solid acid catalyst. The catalyst of the present application is simple to prepare, has high 1-butene trimerization selectivity, and can maintain high activity after long-time operation.

The invention discloses a method for preparing formic acid through water carbonylation, and belongs to the technical field of catalytic chemistry. The method comprises the following steps: heating and vaporizing water, mixing with carbon monoxide to form feed gas, and reacting under the action of a catalyst at certain temperature, pressure and space velocity to generate formic acid. The catalyst is selected from at least one of mordenite, ZSM-5, ZSM-23, a Na-type Y molecular sieve and an H-type Y molecular sieve, and can be subjected to gas activation before use. According to the method, cheap and easily available raw materials are adopted, the reaction condition is mild, the technological process is simple, and a new way with potential application value is provided for green synthesis of formic acid.

The application relates to the technical field of catalyst preparation, in particular to a high-selectivity catalyst suitable for high air speed and a preparation method and application thereof. 12 Bi a Fe b Co c Ni d A e Cl f O x , A is one of sodium, potassium, rubidium and cesium; a=0.3-3, b=1-4, c=3-8, d=1-5, e=0.01-0.5, f=0.01-2, and x is a value determined by the total valence of elements in the general formula except oxygen. The catalyst prepared by the preparation method has excellent catalytic performance under high air speed conditions and has a good application prospect.

The utility model relates to a fixed bed phenol hydrogenation catalyst evaluation device which comprises a reactor, the upper part of the reactor is provided with a feed port, the lower part of the reactor is provided with a discharge port, the discharge port is connected to a condenser through a pipeline, the lower part of the condenser is provided with a gas-liquid two-phase outlet, the gas-liquid two-phase outlet is connected to a gas-liquid separator through a pipeline, and the gas-phase outlet is arranged above the gas-liquid separator. The outlet of the circulating fan is connected to a phenol evaporator through a pipeline, the upper part of the phenol evaporator is provided with a gas phase outlet, the gas phase outlet is connected to a heater through a pipeline, the upper part of the heater is provided with a material outlet, and the material outlet is connected to a material inlet at the upper part of the reactor through a pipeline. The device can accurately adjust the temperature of a reaction hot spot, is suitable for comparison tests of multiple parameters such as system pressure, reaction temperature, hydrogen / phenol feed ratio, air speed and catalyst service life, almost completely fits an industrial device, and greatly improves the accuracy of a catalyst evaluation result.

This invention discloses a method for preparing formaldehyde by oxidizing methylal, belonging to the field of chemical technology. The method uses methylal and oxygen as raw materials, wherein the volume fraction of methylal feed is 2%~6%, the volume ratio of methylal to oxygen feed is 1:1.5~1:5.0, the mass ratio of methylal to water feed is 1:0.09~1:0.24, and the mass ratio of methylal to methanol feed is 1:0.02~1:0.13; the oxidation reaction temperature is 280℃~380℃, and the gas hourly space velocity is 6000~11000 h⁻¹. ‑1 This system regulates reaction selectivity through the synergistic effect of water vapor and oxygen; simultaneously, the staged introduction of methanol not only increases the reaction temperature at the top of the reactor and balances the temperature distribution throughout the reactor, but also achieves efficient control of the heat of reaction, thereby reducing methanol residue in the product. This invention effectively solves the problems of low reaction temperature and high methanol content in the product during the oxidation of methyl acetal, and has the advantages of excellent formaldehyde selectivity and high product purity.

The application relates to the technical field of denitration, and specifically discloses a lime kiln flue gas denitration treatment method. The lime kiln flue gas denitration treatment method specifically comprises the following steps in sequence: SNCR and SCR; the process parameters of the SNCR section are as follows: the flue gas temperature is 900-1200 DEG C, 10-14 wt% urea solution is sprayed, and the target denitration efficiency is 10-30%; the process parameters of the SCR section are as follows: the flue gas temperature is 180-220 DEG C, 17-22 wt% ammonia water is used as a reducing agent, a honeycomb catalyst is used, and the space velocity is 3000-5000 h-1 1 ; the honeycomb catalyst is prepared from the following components: vanadium pentoxide, titanium dioxide, zinc-aluminum hydrotalcite and stearic acid. The technical scheme provided by the application has excellent denitration performance in the denitration treatment of lime kiln flue gas; the denitration system can be operated for a long time, and the denitration efficiency is relatively high after long-time continuous operation.

The invention belongs to the technical field of alkane processing, and particularly relates to a process for preparing n-pentene from n-pentane, which comprises an n-pentane dehydrogenation device, an n-pentene separation device and an isomerization reaction and circulation separation device. The n-pentene separation device is used for separating hydrogen flow G-H2 and unreacted n-pentane gas flow M1 from the cooled dehydrogenated gas flow from the n-pentane dehydrogenation device, separating n-pentene gas flow P-2, and sending the n-pentene gas flow P-2 to the isomerization reaction and circulation separation device for treatment; the isomerization reaction and cyclic separation device comprises a pentene separation tower, a 2-pentene heavy component removal tower and a 2-pentene isomerization reactor group; the isomerization reactor group is provided with 2-3 fixed bed reactors VI filled with a 2-pentene isomerization catalyst in parallel; the operation conditions of each reactor VI are as follows: the temperature is 375-390 DEG C, the pressure is 0.05-0.15 MPa, and the mass space velocity of 2-pentene is 1-2h <-1 >. The process provided by the invention has a certain application prospect.

The present application belongs to the technical field of low-temperature denitration catalyst performance evaluation, and particularly relates to a denitration reactor with adjustable volume, a low-temperature denitration catalyst measuring system and a method. The denitration reactor comprises a cylinder and a heating component arranged on the outer wall of the cylinder, and the upper part and the lower part of the cylinder are respectively provided with a gas inlet and a gas outlet. A support rod is fixed to the inner side of the bottom of the cylinder, and a lining plate with adjustable fixed position is arranged on the support rod. In use, the fixed position of the lining plate on the support rod is adjusted so that the center position of the catalyst bed layer above the lining plate is at the same level as the center of the heating component, and the lining plate divides the cylinder into two cavities, and the upper cavity is a denitration reaction zone. The denitration reactor has a movable lining plate inside, and the volume of the denitration catalyst reaction can be changed by moving the lining plate during use, so that the to-be-tested catalyst is always located at the center position of the uniform temperature zone, and the low-temperature denitration catalyst can be tested in a large range of space velocities.

This invention discloses a method for preparing a ruthenium-based catalyst for the catalytic oxidation of hydrogen chloride to chlorine in a fixed-bed reactor and its application. The active component RuO2 of the catalyst is loaded onto the surface of a TiO2 support through precursor salt adsorption-deposition-calcination, and then shaped into a ruthenium-based catalyst that can be directly used in a fixed-bed reactor by adding structural and molding aids. The ruthenium-based catalyst exhibits high low-temperature activity when used for the catalytic oxidation of hydrogen chloride to chlorine: at 280°C and a space velocity of 0.75 g-HCl / (g-cat·h), the conversion rate of hydrogen chloride can reach 90% to 95%. Compared with the current operating temperature of industrial fixed-bed reactors, the reaction temperature can be reduced by at least 20°C, while the conversion rate of hydrogen chloride can be increased by 5% to 10%.

Systems and methods to integrate product stabilization directly into the plasma conversion system are provided herein. The system includes a catalyst bed located downstream of the plasma reactor. The plasma reactor produces saturated and unsaturated hydrocarbons and hydrogen. The plasma effluent flows directly into a catalyst bed containing catalyst, which helps to provide process stability for species in the plasma effluent while they retain plasma-induced activation. The hydrogenation efficiency is controlled mostly by the catalyst bed temperature and space velocity. The stabilized product is sent to a separator unit where the liquid and gas products are separated for further processing.

The invention belongs to the technical field of sustainable aviation fuel preparation processes, and provides a green method for preparing sustainable aviation fuel through propylene oligomerization-hydrogenation. The method comprises the following steps: dehydrating, desulfurizing and purifying green propylene, performing selective oligomerization in a fixed bed reactor by adopting a solid acid catalyst at the temperature of 70-180 DEG C, under the pressure of 2-5MPa and at the air speed of 1-3h <-1 > to prepare an olefin oligomer, and rectifying to obtain unreacted propylene and lt; c6 olefin is separated and mixed with fresh propylene for recycling, the obtained C9-C15 olefin passes through a fixed bed reactor, a nickel-based catalyst is adopted for catalytic hydrogenation, the temperature is controlled to be 60-150 DEG C, the pressure is controlled to be 1-3 MPa, the H2 / olefin molar ratio is controlled to be 2: 1-3: 1, the air speed is controlled to be 1-3 h <-1 >, it is ensured that olefin is completely saturated while cracking is avoided, after a product is subjected to gas-liquid separation, gas-phase H2 is recycled, and the C9-C15 olefin is recycled. And rectifying the liquid phase to obtain the sustainable aviation fuel meeting the ASTMD7566 standard.

The application discloses an industrial platinum group metal deoxidation catalyst, which comprises an active component and a carrier; the active component is one or a combination of two or more of ruthenium, rhodium, palladium, osmium, iridium and platinum, and the content of the active component is 0.02-0.4 wt% of the weight of the carrier; and the carrier is a gamma-alumina ball with a specific surface area of not less than 200 m 2 / g, a pore volume of 0.3-0.6 mL / g and a particle size range of 3-6 mm. The industrial platinum group metal deoxidation catalyst provided by the application adopts cheap and readily available industrial gamma-alumina balls as the carrier, and the high specific surface area of the gamma-alumina balls improves the deoxidation performance of the deoxidation catalyst, so that the deoxidation reaction can be smoothly carried out at low temperature and normal pressure; and the catalyst still has high-precision deep deoxidation effect on trace oxygen of 300-500 ppm in industrial hydrogen under the condition that the space velocity is greater than or equal to 10000 h ‑1 , so that the outlet oxygen is less than 1.0 ppm, and the catalyst is suitable for large-scale and efficient deoxidation of industrial hydrogen in industrial production.

The invention relates to a post-combustion carbon dioxide trapping system based on a solid adsorption method and a reaction strengthening method. The system adopts a helical surface to intensify and form an adsorbent. The after-combustion carbon dioxide capture reaction strengthening method based on the solid adsorption method is used for CO2 capture of a fixed bed system, and comprises the following steps: introducing a mixed gas containing CO2 into a fixed bed reactor loaded with the helical surface reinforced forming adsorption, and completing CO2 adsorption at 600-750 DEG C, normal pressure and air speed of 6000-20000 h <-1 >; the invention provides a solution with high stability and excellent adsorption performance for adsorption and separation of CO2 in high-temperature industrial flue gas.

This invention provides a selective hydrogenation method for cracked gasoline fractions, in which the cracked gasoline fractions and hydrogen are hydrogenated in a fixed-bed reactor at a temperature of 30–100°C, a pressure of 2.0–5.0 MPa, and a feed volume hourly space velocity of 0.8–3.5 h⁻¹. ‑1 The hydrogen-to-oil volume ratio is 80–300:1; the catalyst support is alumina with a bimodal porous structure; the active components include Pd, Pt, Ce, W, Ni, and Cu, with Pd content of 0.2–0.5%, Pt content of 0.02–0.15%, Ce content of 0.5–4.0%, W content of 0.2–2.5%, Ni content of 0.5–5.0%, and Cu content of 0.5–3.0% by catalyst mass. Ni-Cu is supported by a microemulsion method, while Pd, Pt, Ce, and W are supported by a solution method, with Pt and Ce being supported simultaneously. This hydrogenation method exhibits excellent hydrogenation activity, anti-coking properties, and regeneration performance.

The present invention relates to a supported catalyst comprising a support and 0.1 to 10 wt. % of tantalum, calculated as Ta2O5 and based on the total weight of the catalyst, wherein the supported catalyst further comprises from 50 to 350 ppm of aluminium and from 1 to 50 ppm of sodium, based on the total weight of the catalyst, respectively. Moreover, the invention relates to a catalyst reaction tube for the production of 1,3-butadiene comprising at least one packing of the supported catalyst as defined herein, to a reactor for the production of 1,3-butadiene comprising one or more of the catalyst reaction tubes as defined herein, and to a plant for the production of 1,3-butadiene comprising one or more of the reactors as defined herein. The invention also relates to a process for the production of 1,3-butadiene as defined herein and to a process for the production of the supported catalyst as defined herein. Finally, the present invention relates to the use of the supported catalyst as defined herein for the production of 1,3-butadiene from a feed comprising ethanol and acetaldehyde and to the use of aluminium in an amount in a range of from 50 to 350 ppm in a supported catalyst for the production of 1,3-butadiene from a feed comprising ethanol and acetaldehyde for increasing the 1,3-butadiene productivity of the catalyst.

The invention provides a method for preparing trifluorotoluene by applying a defluorination-preventing palladium-carbon catalyst to fixed bed catalytic hydrogenation, which comprises the following steps: filling a fixed bed reactor with a palladium-carbon catalyst, sealing, and continuously introducing hydrogen; a chlorobenzotrifluoride compound is continuously introduced, the reaction temperature is 240-260 DEG C, and the mass space velocity of the chlorobenzotrifluoride compound is 0.6-1.25; and collecting the dechlorinated hydrogenation reduction material after the reaction is finished, and purifying to obtain the benzotrifluoride. The method for preparing trifluorotoluene by applying the defluorination-preventing palladium carbon catalyst to fixed bed catalytic hydrogenation is high in yield, less in three wastes, low in cost and high in safety.

This invention discloses a method for removing alkynes via C2 hydrogenation, particularly under high C4 conditions. Using a hydrogenation catalyst, the overhead effluent from the pre-propane stripper in an ethylene plant is selectively hydrogenated in a three-stage tandem reactor in an adiabatic bed to remove alkynes and dienes. Reaction conditions: reactor inlet temperature 50–100°C, pressure 1.5–4.5 MPa, space velocity 8000–20000 h⁻¹. ‑1 The preferred reaction conditions are: inlet temperature 60–90℃, pressure 2.5–4.0 MPa, and volumetric hourly space velocity 10,000–14,000 h⁻¹. ‑1 The catalyst support is alumina or primarily alumina, exhibiting a bimodal pore structure. The catalyst contains at least Fe, Pd, 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 Ni, Cu, and Pd supported in the microemulsion are mainly distributed within the macropores of the support. This catalyst exhibits a low reduction temperature and excellent catalytic performance and anti-coking properties.

The application discloses a catalytic cracking gasoline hydrofining method, which comprises the following steps: loading a pre-sulfided hydrofining catalyst into a fixed bed reactor, sulfidizing the hydrofining catalyst, mixing and preheating catalytic cracking gasoline and hydrogen, and then feeding the mixture into the fixed bed reactor to react, wherein the reaction conditions are as follows: the reaction temperature is 240-360 DEG C, the reaction pressure is 1.5-4.0 MPa, the space velocity is 0.5-4 h-1, and the hydrogen / oil volume ratio is 100-600:1. ‑1 The preparation method of the hydrofining catalyst is as follows: performing atomization and spraying treatment on a carrier by using a pre-spraying solution, aging after the spraying is completed to obtain a pretreated carrier, wherein the pre-spraying solution is a citric acid aqueous solution or a potassium hydroxide solution; impregnating the pretreated carrier with an impregnation solution containing an active component, and then aging, drying and calcining to obtain the hydrofining catalyst.

The application provides a selection method of carbon di-fragment, and the reaction process conditions are as follows: reactor inlet temperature is 55-110 DEG C, reaction pressure is 1.5-3.0 MPa, gas volume space velocity is 1000-5000 h ‑1 : the hydrogen at the reactor inlet is from crude hydrogen, the CO content in the crude hydrogen is 0.1%-1%, the hydrogen / acetylene volume ratio is 1.3-3.0, the catalyst used in the hydrogenation method is a catalyst with non-noble metal Fe as the main active component, through the combination of the catalyst and the reaction process conditions, the sensitivity of the reaction temperature to the CO content in the hydrogenation process is reduced, and the catalyst cost and the coking amount of the catalyst are reduced while the selection hydrogenation efficiency of the carbon di-fragment is ensured.

The invention relates to a method for preparing ethyl acetate through ethanol dehydrogenation. According to the method, ethanol or an ethanol aqueous solution is adopted as a reactant, and under the catalytic action of a CuZn-based composite metal oxide catalyst, the ethyl acetate is prepared through an anaerobic dehydrogenation reaction. The reaction conditions are as follows: the reaction is carried out in a fixed bed reactor, the reaction pressure is 0.3-3MPa, the reaction temperature is 160-260 DEG C, and the ethanol feeding mass space velocity is 0.5-4h <-1 >. The method is characterized in that a ZnO auxiliary agent is added on a copper-based catalyst and is used for preparing ethyl acetate through ethanol dehydrogenation, and meanwhile, high-purity H2 with the purity of gt is produced as a byproduct; the conversion rate can be up to 80%, and the selectivity of ethyl acetate can be up to 96%.

The invention relates to a method for preparing formaldehyde through methanol oxidation. According to the method, methanol is taken as a raw material, oxygen-containing mixed gas is taken as an oxidant, and formaldehyde is generated through oxidation reaction under the action of a catalyst. An iron-vanadium composite metal oxide catalyst is adopted in the reaction, corresponding metal salt is used as a precursor, a precipitator is dropwise added to adjust the pH value to obtain a suspension, and the catalyst is finally prepared through filtering, washing, drying and roasting. The specific reaction process is as follows: the catalyst is molded and then loaded into a reaction tube, the reaction tube is placed in a fixed bed reactor, methanol is fed by a pump, and the reaction temperature is 190-260 DEG C and the volume space velocity is 6000-10000 h <-1 > under normal pressure. The method is characterized in that the iron-vanadium composite metal oxide catalyst is used for preparing formaldehyde through methanol oxidation, the methanol conversion rate can reach 95%, the formaldehyde selectivity reaches up to 92%, high activity, selectivity and stability are shown, and potential industrial application prospects are achieved.