1221results about "Catalysts" patented technology

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

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.

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 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 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.

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.

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.

The invention relates to a process for the production of ethylene by oxidative dehydrogenation (ODH) of ethane, comprising: a) supplying ethane and oxygen to a first ODH zone which is formed by multiple reactor tubes containing a mixed metal oxide ODH catalyst bed; b) contacting the ethane and oxygen with the catalyst resulting in multiple effluent streams, wherein the multiple reactor tubes are cooled by a coolant; c) mixing at least a portion of the multiple effluent streams from step b) resulting in a mixture comprising ethylene, unconverted ethane and unconverted oxygen; d) supplying at least a portion of the mixture from step c) to a second ODH zone containing a mixed metal oxide ODH catalyst bed; e) contacting at least a portion of the mixture from step c) with the catalyst in the second ODH zone resulting in a stream comprising ethylene and unconverted ethane.

A catalyst and a method for producing the catalyst are provided. An exemplary catalyst is of the formula: Mo a V b Bi c M d O x This formula includes: In this formula, M is Ta or Nb, a is 1.0, b is 0.01 to 0.5, c is 0.005 to 0.2, d is 0.005 to 0.1, and x is the number of oxygen atoms required to make the catalyst electrically neutral. The values ​​of a, b, c, and d are determined based on the amount of each starting material used to form the catalyst. The catalysts provided herein may be suitable as catalysts in oxidative dehydrogenation reactions, such as the oxidative dehydrogenation of ethane.

Disclosed herein is a method for converting ethanol to 1,3-butadiene, wherein the method utilizes H2 produced during a first step of the method for subsequent conversions involved in the method. In particular aspects, H2 produced from converting ethanol to acetaldehyde is used to promote the conversion of the acetaldehyde to 1,3-butadiene. The H2 promotes enhanced catalyst stability, as well as enhanced selectivity and yields of the 1,3-butadiene product. In particular aspects, the method comprises two steps to produce the 1,3-butadiene from the ethanol and H2 produced from a first step facilitates enhanced selectivities and yields for the second step.

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: (R1)(R2)A-X-C(R3)(R4). A and C may be phosphorus. X may be B(R5), Si(R5)2, N(R5), wherein R5 is an aryl group substituted with a halogen, halogenated alkyl or a silyl group, and wherein B, or N, or Si is bound to A and C. R1, R2, R3, and R4 may be independently chosen hydrocarbyl groups or heterohydrocarbyl groups.

The venturi-type scrubber may be used in conjunction with the removal of solids and quench gas-phase reaction products from the gas-phase reaction products. A method can include: providing a reaction product comprising a hydrocarbon gas and a solid; introducing the reaction product into a venturi type scrubber; introducing a scrubbing fluid into the venturi-type scrubber, wherein the scrubbing fluid is at a lower temperature than the reaction product; generating, by the venturi scrubber, a heterogeneous product comprising a scrubbed reaction product and a waste scrubbing fluid, the scrubbed reaction product comprising the hydrocarbon gas, and the waste scrubbing fluid comprising the scrubbing fluid and the solids; and separating the hydrocarbon gas from the multiphase fluid. A system may include a reactor; a venturi-type scrubber having a first inlet fluidly connected to the reactor and a second inlet configured to receive a scrubbing fluid; and a separation column configured to receive a multiphase stream from the venturi scrubber after solids are removed.

Bis-phosphites having 2-phenylphenol flanking structural units and their use in hydroformylation.

Systems and methods of producing 1-hexene are disclosed. The methods include oligomerizing ethylene to produce 1-hexene in a reactor unit, which involves flowing a first solvent system into the reactor unit, the first solvent system adapted to improve selectivity of 1-hexene in the oligomerizing of the ethylene. The methods can include flowing part of a second solvent system into the reactor unit under washing mode, the second solvent system adapted to dissolve by-products in the reactor unit being washed. The methods can include flowing part of a second solvent system into the catalyst preparation unit, the second solvent system adapted to dissolve catalysts in the catalyst preparation step. The systems can include a reactor, a wax / polymer removal unit, and at least two C6 distillation columns in series for producing 1-hexene.

The present application provides a method for preparing a deuterated chemical by means of a deuteration reaction of a carbon-hydrogen bond with a deuterium gas under the catalysis of an alkali, wherein in the presence of a catalyst, a deuterium gas is added into a compound containing a carbon-hydrogen bond for a deuteration reaction so as to generate a deuterated compound. A deuterium gas is used as a deuterium source, such that multiple water separation operations, tedious steps and the wasting of energy caused by usage of a large amount of deuterium oxide as a deuterium source are avoided. Moreover, a cheap and easily available alkali metal compound is used for replacing an expensive transition metal catalyst and a complex-structure ligand as a catalyst for a deuteration reaction, and the alkali metal compound has the advantages of a low cost, a good compatibility with functional groups of a substrate and a high deuteration rate. The present application provides a new, low-cost, green and efficient deuteration method, which has a high application value.

Provided is a method for producing a cyclic olefin compound, including a step of producing a cyclic olefin compound by acting a divalent nickel complex represented by General Formula (1) to decarbonylate and decarboxylate an alicyclic dicarboxylic acid anhydride, in which the divalent nickel complex includes at least one specific anionic ligand Y.         Ni(Y)m(L)n     (1) (here, Ni is divalent nickel, Y is an anionic monodentate or polydentate ligand and has at least one Ni-E covalent bond, E is a heteroatom or a π-bonding group, m is 1 or 2, L is a neutral ligand, and n is a real number of 0 to 6)

The disclosure provides an MTW framework-type molecular sieve with crystallites having an average size of 70nm or below. The sieve includes a structure-directing composition comprising 2-pyrrolidone or its N-alkyl derivative and a quaternary ammonium cation. A method for preparing the sieve and its use in producing olefins from alkanes are also described.

This invention relates to a catalytically active or activatable mixture for use in a chemical reactor, comprising: (i) a shaped catalyst body containing a catalytically active or activatable material, and (ii) a conductor, wherein the shaped catalyst body has a characteristic diameter d. cat With the diameter d of these conductors con The ratio between (d) cat / d con The value is in the range of 1.5 to 3, and these shaped catalyst bodies have a characteristic diameter d in the range of 1 mm to 50 mm. cat Furthermore, the diameter of the unformed conductor is the average diameter determined by sieving according to DIN 66165, and the characteristic diameters of the formed catalyst body and the formed conductor are defined as the diameter d of the circumscribed sphere surrounding the formed body. css The sphericity Ψ of the convex hull of the molded body ch The product of the two. The invention further relates to a method for preparing the catalytically active or activatable mixture, the use of the catalytically active or activatable mixture in a chemical reactor as part of or as a directly electrically heated catalyst bed, and a chemical reactor for carrying out a chemical reaction, the chemical reactor containing or comprising the catalytically active or activatable mixture. The invention further relates to a method for carrying out a chemical reaction catalyzed by a shaped catalyst body of the catalytically active or activatable mixture.

A process for dimerizing and oligomerizing olefins to distillate fuels which utilizes a solid acid catalyst for ethylene oligomerization in a first stage and a metal catalyst for further oligomerization in a second stage. Distillate fuels can be produced from the process. Oligomerized olefins may be recycled to the first stage oligomerization reaction to ensure sufficient oligomerization of smaller olefins.

To provide a method for producing ethylene in high yield by selective hydrogenation of a gas mixture containing high-concentration acetylene generated by a methane pyrolysis process.SOLUTION: There is disclosed a process for converting methane into value-added compounds, wherein a gas mixture containing high-concentration acetylene as well as hydrogen formed through methane pyrolysis (for example, non-oxidative coupling of methane) is selectively hydrogenated in the presence of a bimetallic supported catalyst to obtain ethylene from acetylene in the gas mixture, while unreacted methane and hydrogen are recovered as byproducts and / or additionally recycled.SELECTED DRAWING: Figure 1

The present invention relates to cationic molybdenum and tungsten complexes containing a heterocyclic nitrogen carbene (NHC) and preferably a halogen-containing aryloxy ligand. The catalysts are active in olefin metathesis reactions and provide for E-selectivity.

The conversion of nootkatol to nootkaten in the terpene blend is mitigated or prevented by substantially or completely separating the nootkatol, such as α-nootkatol, from compounds present in the terpene blend that catalyze the chemical reaction of nootkatol to nootkaten, and / or by neutralizing at least a portion of the compounds present in the terpene blend that catalyze the chemical reaction of nootkatol to nootkaten. Also disclosed are methods of preparing the terpene blend, the terpene blend, flavor compositions containing the terpene blend, beverages and foodstuffs containing the flavor compositions, fragrance compositions containing the terpene blend, and fragranced products containing the fragrance compositions.

This invention relates to the field of catalyst technology, specifically to an iron-based catalyst, its preparation method and application, and the FTO reaction. The catalyst comprises a support and an active component. The active component, expressed as an oxide, has the following general chemical formula: Fe 100 Mn a Nb b Cs c A d B e O x A is selected from Group VIII nonferrous metals and / or Group VIB elements; B is selected from La series elements; the value of a ranges from 30.0 to 130.0; the value of b ranges from 1.0 to 20.0; the value of c ranges from 0.1 to 10.0; the value of d ranges from 1.0 to 60.0; the value of e ranges from 0.1 to 10.0; x is the total number of oxygen atoms required to satisfy the oxidation states of each element in the catalyst. The iron-based catalyst of this invention exhibits excellent resistance to carbon deposition during use, and when used in the FTO reaction, it can achieve high CO feedstock conversion and C2-C4 olefin selectivity.

A method of selectively producing oligomers can include contacting at least one antifouling agent with a first amount of at least one aluminum alkyl compound to form at least one antifouling compound comprising the following structure or dimer form thereof: (I); and adding the at least one antifouling compound, an additional amount of the at least one aluminum alkyl compound, the at least one titanate compound, and ethylene to a jet loop reactor to oligomerize the ethylene to produce one or more of 1-butene, 1-hexene, or 1-octene. (I)

The invention relates to a method for producing styrene, starting from ethylbenzene, the method in particular involving the process of transferring heat from the obtained product gas flow to an H2O-containing flow. It has been found that the present method for producing styrene allows the heat required to carry out the dehydrogenation reaction to be efficiently recycled, in particular in order to heat the H2O-containing input flow being used.

The present invention provides a system and a process for the production of methane, C2-C100 linear alkanes, C2-C10 olefins, oxygenates, methanol and combinations thereof, comprising: an oxyfuel combustor comprising a combustion gas outlet, and a first fluid entrance; a heat recovery system; a carbon capturing unit comprising an adsorption column which comprises a combustion gas inlet in fluid communication with the combustion gas outlet of the oxyfuel combustor, and a feed gas inlet; a desorption column; one or more methanol synthesis reactors; wherein the adsorption column comprises a base portion and a top portion; the adsorption column extends a height from the base portion to the top portion; the base portion corresponds to one half of the height of the adsorption column; the feed gas inlet and the combustion gas inlet are located in the base portion; and the feed gas inlet is located above the combustion gas inlet in the base portion.

A fluidized bed device for coupling naphtha and methanol to prepare aromatics and co-produce olefins and its application method are provided. By using the device, under the action of a catalyst, naphtha reacts with methanol to generate product gas containing aromatics and light olefins as main components. The method can efficiently and selectively convert linear and branched aliphatic hydrocarbons into aromatics, while also increasing p-xylene production through aromatic methylation reactions, with the p-xylene content in the xylene mixture exceeding 75 wt %. The fluidized bed reactor achieves increased p-xylene production by controlling the progression of cascade reactions (naphtha→benzene / toluene→p-xylene). Additionally, it utilizes the methylation reaction of benzene / toluene with methanol to provide in-situ heat for the coupled naphtha-methanol aromatization process, thereby achieving autothermal balance.