2065results about "Catalysts" patented technology

A process for converting an ethanol feed stream to ethylene, comprising passing a portion of said ethanol feed stream to two reactors in parallel and then passing the combined product to a third reactor operated at a higher temperature to prevent the formation of ethers such as diethyl ether.

The invention belongs to the field of photocatalytic materials, and particularly relates to a high-entropy sulfide and a preparation method and application thereof. The high-entropy sulfide is granular, the molecular general formula is (MnaFebCocCudZe) xS, x is equal to 1, and the atomic ratio of Mn to Fe to Co to Cu to Zn is a: b: c: d: e of (1-2): (1-2): (1-2): (1-2): (1-2): (1-2): (1-2). The preparation method comprises the following steps: S1, dissolving metal salt in a mixed solvent of isopropanol and glycerol according to the atomic ratio of metal elements, and carrying out solvothermal reaction to obtain a precursor; and S2, dispersing the precursor in ethanol, adding thioacetamide as a sulfur source, and carrying out solvothermal reaction to obtain the high-entropy sulfide. The high-entropy sulfide disclosed by the invention is used as a photocatalytic material and shows excellent photocatalytic performance.

Provided herein are systems and methods for converting CO2 and a reduction gas, such as H2 or a hydrocarbon, using a reduction catalyst and an aromatic catalyst into mixtures of paraffins, and aromatics for use as aviation fuel. The reduction catalyst and aromatic catalyst, and systems and methods incorporating the same, provide advantages over other methods in the art related to increased yield, catalyst stability and longevity.

The present invention belongs to the technical field of design and synthesis of carbon-monoxide and carbon-dioxide-based Fischer-Tropsch synthesis catalysts, and discloses a novel iron-based Fischer-Tropsch synthesis catalyst containing both iron and carbon and a synthesis method and use thereof. The present invention specifically relates to a catalyst mixture for use in hydrogenation of CO and / or CO2, which catalyst mixture comprises i) iron oxide promoted by alkali metal, alkaline earth metal or transition metal, and ii) iron carbide. The invention further relates to a method for production of iron carbide composite comprising different iron carbides, and the use of said carbide composite in combination with alkali metal, alkaline earth metal or transition metal promoted iron oxide for use in hydrogenation of CO and / or CO2.

Transalkylation processes using catalysts comprising three dimensional 12 membered ring zeolites with a combination of small and large pores are described. These catalysts have increased conversion of alkylphenols to phenol, cresols, and alkylbenzenes from coal-derived liquid streams compared to catalysts consisting of HZSM-5 zeolite.

A process for dehydrating ethanol to produce ethylene is provided. The ethanol is dehydrated to produce ethylene, which is subsequently converted to longer-chain olefins, which are then hydrogenated to produce long-chain paraffins. In some embodiments, a split feed is used to improve efficiency, eliminating the caustic wash column. Advantages of the process include lower steam requirements and a 30-40% reduction in combined reactor volume when using two reactors compared to a single reactor.

A method may include operating a dehydrogenation process whereby a hydrocarbon-containing feed is converted to light olefins, wherein the dehydrogenation process utilizes a fluidized process catalyst that circulates between a reactor and a combustor. The method may comprise withdrawing the process catalyst from the dehydrogenation process, modifying the process catalyst to form a modified catalyst, and adding the modified catalyst back to the dehydrogenation process. The process catalyst may include from 0.1 wt. % to 10 wt. % of one or more metals chosen from gallium, indium, thallium, or combinations thereof, from 1 ppmw to 1000 ppmw of one or more metals chosen from platinum, palladium, rhodium, iridium, ruthenium, osmium, or combinations thereof, and at least 85 wt. % support. Modifying the process catalyst may include adding one or more of manganese, iron, chromium, or vanadium.

A machine learning model predicts a K value for a new iron ethylene oligomerization catalyst structure, where the K value has not yet been experimentally determined. The system utilizes a device comprising memory coupled to at least one processor, the memory having instructions that cause the at least one processor to: input a set of reaction conditions and a new iron ethylene oligomerization catalyst structure comprising a ligand to a random forest machine learning regressor model, wherein the random forest machine learning regressor model is trained on a data set comprising multi-dimensional features for tested iron ethylene oligomerization catalyst structures, wherein the multi-dimensional features comprise experimental K values, physical features, molecular features, and connective steric factors for each of the tested iron ethylene oligomerization catalyst structures

The invention discloses a method for preparing 1, 3-butadiene, and the method comprises the following steps: enabling a raw material containing gamma-valerolactone to be in contact and react with a catalyst to obtain the 1, 3-butadiene, the catalyst is a hydrogen type molecular sieve with a ten-membered ring topological structure, and the typical topological structure types of the catalyst comprise FER, TON, MTT, EUO, * MRE, MEL and MWW. In a fixed bed reactor, gamma-valerolactone is taken as a raw material and passes through the reactor from top to bottom. The target product 1, 3-butadiene can be efficiently prepared under the condition of 300-450 DEG C by using the catalyst.

A process for preparing middle distillates from an olefinic feedstock, bya) oligomerization fed with the olefinic feedstock, a first recycle and a second recycle, and operated in the presence of at least one oligomerization catalyst, to produce a reaction effluent containing dimers, trimers and oligomers;b) fractionating the reaction effluent into:a light fraction containing at least part of the unconverted olefinic feedstock;an intermediate fraction containing at least part of the dimers and trimers; anda heavy fraction containing the oligomers;c) recycling by the preparation of a first recycle containing at least part of the light fraction; and a second recycle containing at least part of the intermediate fraction; and transfer of the first recycle and the second recycle to step a);d) hydrogenating at least part of the heavy fraction.

Methods for preparing catalysts for oxidative dehydrogenation (ODH) of alkanes such as ethane are provided. An exemplary method includes forming a slurry including metal oxides; one or more of a bismuth compound, an antimony compound, and a tellurium compound; a reducing agent; and water; and heating the slurry to form the catalyst. The metal oxides include an oxide of molybdenum and an oxide of vanadium. The bismuth compound includes bismuth oxide, bismuth hydroxide, or a bismuth carbonate. The antimony compound includes an oxide of antimony, an antimony acetate, or an antimony ethoxide. The tellurium compound includes tellurium dioxide. The reducing agent includes molybdenum dioxide and may further include vanadium dioxide. The methods use all inorganic reagents, with no build up COx pressure observed during the hydrothermal synthesis.

The invention discloses an intermittent charging system of a solid catalyst and a charging method of the solid catalyst in a propylene dimerization process. The intermittent feeding system comprises a feeding barrel section, the feeding barrel section comprises an upper barrel section and a lower barrel section, a feeding device is arranged between the upper barrel section and the lower barrel section, the top of the upper barrel section and the bottom of the lower barrel section are provided with a first discharging valve and a second discharging valve respectively, and the side wall of the upper barrel section is provided with a purging gas inlet and an exhaust port; and the charging barrel section is communicated with a charging hole of the reaction kettle. The system and the method provided by the invention not only can meet strict requirements of the process on anhydrous and anaerobic conditions of the catalyst, but also can realize intermittent addition of the catalyst without influencing normal operation of the device, and are convenient to replace.

The present invention relates to a method for preparing, activating and regenerating a metal supported catalyst, comprising: treating a Ma-Mb-Mc metal supported catalyst at 10-700° C. by using an ammonia or nitrogen-containing organic matter, wherein the Ma metal is an active metal selected from one or more of a noble metal atom or a transition metal, the support is a common industrial porous catalyst, and the Ma metal is dispersed on the support in a state of single atomic site. According to the Ma-Mb-Mc metal supported noble metal / zinc catalyst treated by the method of the present invention, the direct dehydrogenation conversion rate and selectivity of catalyzing light alkanes are remarkably improved; the method for preparing the catalyst is simple in process, the catalytic activity after regeneration is still kept, and the catalyst can be industrially produced on a large scale.

Provided is a methanation device for removing a saturated hydrocarbon from a raw material gas containing methane and a saturated hydrocarbon through methanation, in which a saturated hydrocarbon having at least two carbon atoms reacts with hydrogen and the saturated hydrocarbon is converted into methane. The methanation device comprises: at least two catalyst layers composed of a catalyst for methanation, the catalyst layers being provided at intervals in the flow direction of a mixed gas containing a raw material gas and a hydrogen-containing gas; a hydrogen supply line for supplying a hydrogen-containing gas to an upstream side of the catalyst layer on the most upstream side in the flow direction of the mixed gas; a raw material gas supply line for supplying the raw material gas to each space between two catalyst layers adjacent to each other in the flow direction of the mixed gas and the upstream side of the catalyst layer on the most upstream side in the flow direction of the mixed gas; and a cooler provided between two catalyst layers adjacent to each other in the flow direction of the mixed gas and cooling the mixed gas discharged from the catalyst layer on the upstream side among the two catalyst layers adjacent to each other.

A method may include contacting a hydrocarbon-containing feed with a catalyst in a reactor to form an olefin-containing effluent, then at least partially separating the olefin-containing effluent from the catalyst. Passing the catalyst to a combustor and heating the catalyst by combusting a supplemental fuel. The supplemental fuel includes methane in an amount greater than or equal to 1 mol. %. Passing the catalyst from the combustor to the reactor, such that at least a portion of the catalyst continuously cycles between the reactor and the combustor. The catalyst includes from 0.1 wt. % to 10 wt. % of one or more metals chosen from gallium, indium, thallium or combinations thereof, from 5 ppmw to 1000 ppmw of one or more metals chosen from platinum, palladium, rhodium, iridium, ruthenium, osmium, or combinations thereof, from 100 ppmw to 30000 ppmw of chromium, and at least 85 wt. % support.

The invention provides a method for synthesizing 1, 3-butadiene by continuous catalytic conversion of acetylene, which comprises the following steps: S1, continuously introducing acetylene as a raw material into a reactor I for acetylene dimerization catalytic reaction to obtain primary reaction gas containing vinyl acetylene; and S2, continuously introducing the initial reaction gas and hydrogen into a reactor II, and carrying out selective catalytic hydrogenation reaction to obtain 1, 3-butadiene. The technical scheme of the invention provides a continuous catalytic process method, and 1, 3-butadiene is directly synthesized by using acetylene as a raw material through coupling acetylene catalytic dimerization reaction and vinyl acetylene selective catalytic hydrogenation reaction. The obtained product is easy to separate from a catalytic system, and the whole process flow is simple to operate, economical and environment-friendly, and has a good application prospect.

The present invention provides an integrated plasma catalytic system for biogas conversion comprising a plasma treated mesoporous or microporous catalyst and a plasma source for converting biogas containing methane and carbon dioxide to liquid oxygenates rich in methanol or acetic acid. Biogas from different solid wastes can be converted into liquid oxygenates including methanol and acetic acid under normal temperature and pressure conditions.

A reduction catalyst comprising iron and zinc is disclosed having improved selectivity and activity. Methods of making and using the reduction catalyst for carbon dioxide hydrogenation are also disclosed.

A catalyst includes from 5 ppmw to 1000 ppmw of platinum, from 0.1 wt. % to 10 wt. % of gallium, from 2300 ppmw to 30000 ppmw of iron, and at least 85 wt. % support, wherein the support includes one or more of alumina, silica, or combinations thereof.

The method is for producing para-xylene using, as a main raw material, a mixed gas of carbon dioxide or carbon monoxide or both thereof and hydrogen. The method including: a reaction step of bringing a raw material mixed gas including the mixed gas into contact with a reaction catalyst under high temperature and high pressure to cause a reaction, to thereby obtain a product gas mixture containing para-xylene; a separation step of cooling the product gas mixture obtained in the reaction step to condense a high boiling point component, to thereby separate the product gas mixture into a water phase containing a water-soluble component, an oil phase containing a xylene mixture, and a gas phase containing an unreacted gas; and a circulation step of mixing at least part of the gas phase having been separated in the separation step into the raw material mixed gas.

A method of converting a polymer including contacting a catalyst with a low-density polyethylene polymer to form a mixture and heating the mixture to a temperature of 200 degrees Celsius (° C.) to 600° C. in a microwave reactor to form a product. The catalyst includes an HZSM-5 zeolite, and 1 weight percent (wt. %) to 10 wt. % gallium and 0.1% to 5 wt. % copper, based on the total weight of the catalyst.

To provide a methanation apparatus capable of suppressing deterioration of a catalyst for methanation, a methanation method, a direct decomposition apparatus of hydrocarbons, and a direct decomposition method of hydrocarbons.SOLUTION: A methanation apparatus for removing saturated hydrocarbons from a raw material gas by methanation where saturated hydrocarbons having two or more carbon atoms and hydrogen react to convert the saturated hydrocarbons into methane includes at least two catalyst layers 11a, 11b arranged with gaps in between and being catalyst layers for methanation, a hydrogen supply line 3 to provide a hydrogen-containing gas upstream of the most upstream catalyst layer in a circulation direction of a mixed gas, and a raw material gas supply line 4 to supply the raw material gas between an upstream side than the most upstream side catalyst layer and adjacent two catalyst layers, and a cooler 13 that is situated between two adjacent catalyst layers and cools the mixed gas flowing out from the upstream catalyst layer in a circulation direction of the mixed gas among the two adjacent catalyst layers.SELECTED DRAWING: Figure 1

The present invention relates to a PtSn disordered alloy sub-nanometer catalyst for propane dehydrogenation. The catalyst uses γ-Al2O3 nanospheres as a carrier, and the active component Pt is diluted to a single-atom dispersion state by excessive Sn. During the high-temperature H2 reduction process, the Sn atoms around Pt are reduced by the hydrogen spillover effect of Pt atoms, and finally a PtSn disordered alloy sub-nanometer catalyst is formed. Among them, the mass percentage of Pt is 0.01-0.1%, the mass percentage of Sn is 0.08-2%, and the mass ratio of Pt to Sn is 1:10-1:12. This PtSn disordered alloy sub-nanometer catalyst has a simple preparation process and excellent catalytic performance, with high reaction activity and strong stability, and has broad application value in reducing the consumption of precious metals and improving reaction activity.

Catalyst systems suitable for tetramerizing ethylene to form 1-octene may include a catalyst including a chromium compound coordinated with a ligand and a co-catalyst including an organoaluminum compound. The ligand may have a chemical structure according to Formula (1), wherein R1 is a (C3-C20) substituted or unsubstituted hydrocarbyl group; R2, R3, R4, and R5 are independently chosen from (C1-C50) hydrocarbyl groups; and R1 and N are in a cis configuration.

The present invention provides: an ethylene oligomerization method in which an ethylene oligomer is produced by reacting a chromium complex and an organic aluminium compound with ethylene; and the ethylene oligomer thereof.

The present disclosure provides compositions and methods for metathesizing a first alkenyl or alkynyl group with a second alkenyl or alkynyl group, the composition comprising a ruthenium metathesis catalyst and a photoredox catalyst that is activated by visible light.

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.

The present invention relates to the technical field of alcohol dehydration, and specifically to a catalyst for producing alpha-olefins by dehydrating alcohol, a preparation method thereof, and a method for producing alpha-olefins by dehydrating alcohol. The catalyst comprises: 84-99.88 wt% of a main component, 0.04-6 wt% of a Group IIA oxide, 0.05-8 wt% of a Group IIIB oxide, and 0.03-10 wt% of a transition metal oxide; wherein the main component is selected from at least one of Group IVB oxides; and the transition metal oxide is selected from at least one of Group VIB oxides, Group VIII oxides, Group IB oxides, and Group IIB oxides. The present invention rationally modifies the catalyst by introducing Group IIA metal elements, Group IIIB metal elements, and Group VIB, VIII, IB, and IIB metal elements into the main component, thereby suppressing carbon deposition of the catalyst in the alcohol dehydration reaction, improving the catalytic performance of the catalyst, and promoting the efficient conduct of the alcohol dehydration reaction to produce alpha-olefins.

A photochemical process for converting plastics into hydrogen gas, gaseous C1-6 hydrocarbons, and hydrocarbons greater than 6 carbons using light absorbing metal-based catalysts on a solid support under ambient conditions is disclosed.

A catalyst suitable for dehydrogenation of hydrocarbons may include from 0.0005 wt.% to 0.1 wt.% of platinum, palladium, rhodium, iridium, ruthenium, osmium, or combinations thereof; from 0.1 wt.% to 10 wt.% of gallium, indium, thallium, or combinations thereof; from 0.1 wt.% to 5 wt.% of lanthanum, yttrium, or zirconium; at least 85 wt.% support, and from 0 wt.% to 0.001 wt.% cerium.