Catalysts For The Conversion Of Hydroxypropionic Acid Or Its Derivatives To Acrylic Acid Or Its Derivatives

Catalysts for dehydrating hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof to acrylic acid, acrylic acid derivatives, or mixtures thereof with high yield and selectivity, short residence time, and without significant conversion to undesired side products, such as, for example, acetaldehyde, propionic acid, and acetic acid, are provided. The catalysts are mixed condensed phosphates. Methods of preparing the catalysts are also provided.

Catalytic Conversion Of Lactic Acid To Acrylic Acid

Disclosed herein is the catalytic dehydration of lactic acid to acrylic acid, which is characterized by a high conversion of lactic acid, a high selectivity for acrylic acid, a high yield of acrylic acid, and correspondingly low selectivity and molar yields for undesired by-products. This is achieved with a particular class of catalysts defined by a mixture of metal-containing phosphate salts that together provide the catalyst with a very high basicity density and low acidity density. Further, the catalyst is believed to be stable and active for lengthy periods heretofore unseen in the art for such dehydration processes.

Catalytic oxidation method and method for producing conjugated diene

An object of the present invention is to suppress performance deterioration of a molybdenum composite oxide-based catalyst at the time of performing gas-phase catalytic partial oxidation with molecular oxygen by using a tubular reactor. The present invention relates to a catalytic oxidation method using a tubular reactor in which a Mo compound layer containing a Mo compound and a composite oxide catalyst layer containing a Mo composite oxide catalyst are arranged in this order from a reaction raw material supply port side and under a flow of a mixed gas containing 75 vol % of air and 25 vol % of water vapor at 440° C., a Mo sublimation amount of the Mo compound is larger than a Mo sublimation amount of the Mo composite oxide catalyst under the same conditions.

MULTI-METALLIC CATALYST DOPED WITH PHOSPHORUS AND A LANTHANIDE

The invention relates to a catalyst comprising a support, at least one noble metal M, tin, phosphorus and at least one lanthanide group element, the content of phosphorus element being comprised between 0.4 and 1% by weight, and the content of lanthanide group element(s) being less than 1% by weight with respect to the weight of the catalyst. The invention also relates to the process for the preparation of the catalyst and the use thereof in reforming. 1. Catalyst comprising a support , at least one noble metal M , tin , phosphorus and at least one lanthanide group element , the content of phosphorus element being comprised between 0.4 and 1% by weight , and the content of lanthanide group element(s) being less than 1% by weight with respect to the weight of the catalyst.2. Catalyst according to claim 1 , in which the content of noble metal M is comprised between 0.02 and 2% by weight with respect to the weight of the catalyst.3. Catalyst according to claim 1 , in which the metal M is platinum or palladium.4. Catalyst according to claim 1 , in which the tin content is comprised between 0.005 and 10% by weight with respect to the weight of the catalyst.5. Catalyst according to claim 1 , in which the content of lanthanide group element is comprised between 0.01 and 0.5% by weight with respect to the weight of the catalyst.6. Catalyst according to claim 1 , in which the lanthanide group element is cerium.7. Catalyst according to claim 1 , in which the Sn/M atomic ratio is comprised between 0.5 and 4.0 claim 1 , the P/M ratio is comprised between 0.2 and 30.0 claim 1 , and the lanthanide(s)/M ratio is comprised between 0.1 and 5.0.8. Catalyst according to claim 1 , in which the support comprises silica claim 1 , alumina or silica-alumina.9. Catalyst according to claim 1 , which additionally contains a halogenated compound.10. Catalyst according to claim 9 , in which the content of halogenated compound is comprised between 0.1 and 8% by weight with respect to the weight ...

CATALYST FOR METAL MERCURY OXIDATION REACTIONS AND NITROGEN OXIDE REDUCTION REACTIONS, AND EXHAUST GAS PURIFICATION METHOD

A catalyst for oxidation reaction of metallic mercury and reduction reaction of nitrogen oxide, comprising an oxide of titanium, an oxide of molybdenum, an oxide of vanadium, an oxide of phosphorus and gypsum is obtained by kneading titanium dioxide, ammonium molybdate, ammonium metavanadate, phosphoric acid, gypsum dihydrate and water using a kneader to obtain a paste, applying the paste to a metal lath substrate, and then drying and calcining the resultant. 1. A catalyst for oxidation reaction of metallic mercury and reduction reaction of nitrogen oxide , comprising:an oxide of titanium,an oxide of molybdenum and/or tungsten,an oxide of vanadium,an oxide of phosphorus, andgypsum.2. The catalyst according to claim 1 , wherein a ratio of the dry-based mass of gypsum dihydrate to the mass of the oxide of titanium is 1/99 to 40/60.3. A method for exhaust gas purification claim 1 , comprising bringing an exhaust gas containing metallic mercury claim 1 , nitrogen oxide and sulfur dioxide in contact with a catalyst comprising an oxide of titanium claim 1 , an oxide of molybdenum and/or tungsten claim 1 , an oxide of vanadium claim 1 , an oxide of phosphorus and gypsum to oxidize the metallic mercury and reduce the nitrogen oxide. The present invention relates to a catalyst for oxidation reaction of metallic mercury and reduction reaction of nitrogen oxide, and a method for exhaust gas purification. More specifically, the present invention relates to a catalyst that is capable of accelerating gas phase oxidation reaction of metallic mercury and gas phase reduction reaction of nitrogen oxide, and is also capable of suppressing gas phase oxidation reaction of sulfur dioxide, as well as a method for purifying exhaust gas, which comprises oxidizing metallic mercury and reducing nitrogen oxide.There is concern that metallic mercury contained in flue gas discharged from power stations, factories, automobiles and the like affects the environment. Hence, removal of metallic ...

CATALYTIC BODY COATED WITH METAL OXIDE, METHOD OF MANUFACTURING THE SAME, AND METHOD OF PREPARING 1,3-BUTADIENE USING THE SAME

According to an embodiment of the present invention, there are provided a catalytic body, a method of manufacturing the same, and a method of preparing 1,3-butadiene using the same. The catalytic body includes an inactive support; an intermediate layer disposed on a surface of the inactive support; and an active layer disposed on a surface of the intermediate layer, wherein the active layer includes catalyst powder and a binder. 1. A catalytic body comprising:an inactive support;an intermediate layer disposed on a surface of the inactive support; andan active layer disposed on a surface of the intermediate layer,wherein the active layer includes catalyst powder and a binder.2. The catalytic body of claim 1 , wherein the inactive support has a porosity of 70 vol % or less.3. The catalytic body of claim 2 , wherein the inactive support is of one shape selected from the group consisting of a spherical shape claim 2 , a cylindrical shape claim 2 , a ring shape claim 2 , a platy shape claim 2 , and a combination of two or more thereof.4. The catalytic body of claim 3 , wherein the inactive support is one selected from the group consisting of alumina claim 3 , silica claim 3 , zirconia claim 3 , silicon carbide claim 3 , cordierite claim 3 , and a combination of two or more thereof.5. The catalytic body of claim 1 , wherein the intermediate layer may consist of one selected from the group consisting of alumina claim 1 , silica claim 1 , kaolin claim 1 , TiO claim 1 , ZnO claim 1 , bentonite claim 1 , and a combination of two or more thereof.6. The catalytic body of claim 1 , wherein the intermediate layer has a weight of 3 to 15 g/L with respect to a volume of the inactive support.7. The catalytic body of claim 1 , wherein the catalyst powder is an oxide derived from one selected from the group consisting of iron claim 1 , magnesium claim 1 , manganese claim 1 , zinc claim 1 , bismuth claim 1 , molybdenum claim 1 , and a combination of two or more thereof.8. The catalytic ...

Process For Production Of Acrylic Acid Or Its Derivatives From Hydroxypropionic Acid Or Its Derivatives

Processes for the catalytic dehydration of hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof to acrylic acid, acrylic acid derivatives, or mixtures thereof with high yield and selectivity and without significant conversion to undesired side products, such as, acetaldehyde, propanoic acid, and acetic acid, are provided.

ALKANE OXIDATIVE DEHYDROGENATION AND/OR ALKENE OXIDATION

The invention relates to a process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms, wherein the alkane and/or alkene is contacted with oxygen in the presence of a catalyst comprising a mixed metal oxide and one or more diluents selected from the group consisting of carbon dioxide, carbon monoxide and steam, and wherein the conversion of the alkane and/or alkene is at least 40%. 1. A process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms , wherein the alkane and/or alkene is contacted with oxygen in the presence of a catalyst comprising a mixed metal oxide and one or more diluents selected from the group consisting of carbon dioxide , carbon monoxide and steam , and wherein the conversion of the alkane and/or alkene is at least 40%.2. The process according to claim 1 , wherein the conversion of the alkane and/or alkene is of from 45% to 70%.3. The process according to claim 1 , wherein the diluent comprises carbon dioxide.4. The process according to claim 1 , wherein the diluent comprises from 1 to 100 vol. % of carbon dioxide.5. The process according to claim 1 , wherein the alkane is ethane or propane and the alkene is ethylene or propylene.6. The process according to claim 1 , wherein the catalyst is a mixed metal oxide catalyst containing molybdenum claim 1 , vanadium claim 1 , niobium and optionally tellurium. The present invention relates to a process for alkane oxidative dehydrogenation and/or alkene oxidation.It is known to oxidatively dehydrogenate alkanes, such as alkanes containing 2 to 6 carbon atoms, for example ethane or propane resulting in ethylene and propylene, respectively, in an oxidative dehydrogenation (oxydehydrogenation; ODH) process. Examples of alkane ODH processes, including catalysts and other process conditions, are for example disclosed in U.S. Pat. No ...

AGGLOMERATED ODH CATALYST

Oxidative dehydrogenation catalysts for converting lower paraffins to alkenes such as ethane to ethylene when prepared as an agglomeration, for example extruded with supports comprising slurries of NbO. 2. The agglomerated catalyst according to claim 1 , having a cumulative surface area less than 10 m/g as measured by BET and comprising less than 35 wt % of an non-antagonistic binder.3. The agglomerated catalyst according to claim 2 , having a cumulative pore volume from 0.020 to 0.20 cm3/g.4. The agglomerated catalyst according to claim 2 , having a pore size distribution less than 40% having pore width size less than 200 Angstroms.5. The agglomerated catalyst according to claim 2 , having a percent pore area distribution less than 30% and corresponding percentage of pore volume less than 10%.6. The agglomerated catalyst according to in the shape of a sphere claim 2 , rod claim 2 , ring claim 2 , or a saddle having a size from about 1.3 mm to 5 mm.7. The agglomerated catalyst according to claim 6 , wherein the NbOhydrate is acidified.8. The agglomerated catalyst according to claim 6 , wherein the NbOhydrate is treated with a base.9. The agglomerated catalyst according to claim 8 , in the shape of rods having an aspect ratio from 1 to 5/1.3 having a crush strength up to 110 N/mm.10. The agglomerated catalyst according to claim 8 , in the shape of spheres having a crush strength up to 110 N/mm.11. The agglomerated catalyst according to claim 1 , wherein the NbOhydrate is present in an amount less than 15 wt %.12. The agglomerated catalyst according to claim 1 , wherein the NbOhydrate is present in an amount greater than 15 wt %.19. The process according to claim 18 , wherein in step v) the particles are calcined at a temperature of less than 350° C.20. The process according 19 claim 18 , further comprising spheroidizing rod shaped agglomerated particles at a temperature up to 300° C. and then further calcining the resulting spheres at temperatures up to 600° C.21. ...

OXIDATIVE DEHYDROGENATION CATALYST COMPOSITIONS

Provided in this disclosure are catalyst compositions. The catalyst compositions include an oxidative dehydrogenation catalyst that includes a mixed metal oxide having the empirical formula: 1. A catalyst composition comprising an oxidative dehydrogenation catalyst comprising a mixed metal oxide having the empirical formula:{'br': None, 'sub': 1.0', '0.12-0.49', '0.05-0.25', '0.10-0.20', 'c', 'd, 'MoVTeNbAlO'} c is from 0 to 2.0,', 'd is a number to satisfy the valence of the oxide, and', 'the composition is at least 40 wt. % amorphous as measured by XRD., 'wherein2. The catalyst composition of claim 1 , wherein the composition is from 60 wt. % to 80 wt. % amorphous.3. The catalyst composition of claim 1 , wherein the composition further comprises an adjuvant.4. The catalyst composition of claim 3 , wherein the adjuvant comprises about 30 wt. % to about 90 wt. % of the catalyst composition.5. The catalyst composition of claim 4 , wherein the oxidative dehydrogenation catalyst comprises about 10 wt. % to about 70 wt. % of the catalyst composition.6. The catalyst composition of claim 1 , wherein the mixed metal oxide has the empirical formula:{'br': None, 'sub': 1.0', '0.12-0.49', '0.05-0.17', '0.10-0.20', 'c', 'd, 'MoVTeNbAlO'}wherein c is 0.01 to 2.0.7. The catalyst composition of claim 3 , wherein the adjuvant comprises an alumina.8. The catalyst composition of claim 7 , wherein the alumina comprises a boehmite.9. The catalyst composition of claim 1 , wherein the molar ratio of molybdenum to vanadium in the catalyst composition is from 1:0.12 to 1:0.49 claim 1 , the molar ratio of molybdenum to tellurium in the catalyst composition is from 1:0.05 to 1:0.25 claim 1 , the molar ratio of molybdenum to niobium in the catalyst composition is from 1:0.10 to 1:0.20 claim 1 , and the molar ratio of molybdenum to aluminum in the catalyst composition is from 0.01 to 2.0 claim 1 , as determined by PIXE.10. The catalyst composition of claim 1 , wherein the catalyst composition ...

METHOD FOR PREVENTING OR REDUCING GROWTH OF A MICROORGANISM ON A SURFACE

Methods of synthesizing BiS—CdS particles in the form of spheres as well as properties of these BiS—CdS particles are described. Methods of photocatalytic degradation of organic pollutants employing these BiS—CdS particles and methods of preventing or reducing microbial growth on a surface by applying these BiS—CdS particles in the form of a solution or an antimicrobial product onto the surface are also specified. 17-. (canceled)8. A method for preventing or reducing growth of a microorganism on a surface , the method comprising:{'sub': 2', '3, 'applying BiS—CdS particles onto the surface;'} [{'sub': 2', '3, 'the BiS—CdS particles comprise bismuth(III) sulfide and cadmium(II) sulfide;'}, {'sub': 2', '3, 'the BiS—CdS particles are in the form of spheres; and'}, {'sub': 2', '3, 'the BiS—CdS particles are in contact with the surface for 1-24 hours.'}], 'wherein9. The method of claim 8 , wherein an atomic ratio of bismuth to cadmium in the BiS—CdS particles is in a range of 0.5:1 to 4:1 claim 8 , and an atomic ratio of sulfur to bismuth in the BiS—CdS particles is in a range of 3:2 to 8:1.10. The method of claim 8 , wherein the BiS—CdS particles have a BET surface area of 5-25 m/g claim 8 , a pore size of 10-50 nm claim 8 , and a pore volume of 0.02-0.2 cm/g.11. The method of claim 8 , wherein the BiS—CdS particles are applied onto the surface as a solution comprising a solvent and 1 μg/mL to 50 mg/mL of the BiS—CdS particles relative to a total volume of the solution.12. The method of claim 11 , wherein the solvent comprises dimethyl sulfoxide and water.13. The method of claim 8 , wherein the BiS—CdS particles are applied onto the skin of a subject as an antimicrobial cream comprising 0.01 wt %-50 wt % of the BiS—CdS particles relative to a total weight of the antimicrobial cream.14Acinetobacter baumannii, Enterobacter aerogenes, Escherchia coli, Klebsiella oxytocaKlebsiella pneumoniae.. The method of claim 8 , wherein the microorganism is at least one gram-negative ...

Method for preparing carbon-supported platinum-transition metal alloy nanoparticle catalyst

Disclosed is a method for preparing a carbon-supported platinum-transition metal alloy nanoparticle catalyst using a stabilizer. According to the method, the transition metal on the nanoparticle surface and the stabilizer are simultaneously removed by treatment with acetic acid. Therefore, the method enables the preparation of a carbon-supported platinum-transition metal alloy nanoparticle catalyst in a simple and environmentally friendly manner compared to conventional methods. The carbon-supported platinum-transition metal alloy nanoparticle catalyst can be applied as a high-performance, highly durable fuel cell catalyst.

Nb-doped nickel oxide-zirconia composite catalyst and process for preparing the same

Provided are a Nb-doped nickel oxide-zirconia composite catalyst, and a method for preparing the same. An excellent methane modification reaction is performed by doping a nickel oxide site with niobium, so that alcohol may be prepared at low costs. 1. A Nb-doped nickel oxide-zirconia composite catalyst , wherein the niobium is comprised in an amount of 0.01 to 0.15 mol based on 1 mol of the composite catalyst.2. The composite catalyst of claim 1 , wherein the niobium is niobium dioxide doped on a nickel oxide site.3. The composite catalyst of claim 2 , wherein the nickel oxide is present in a cubic phase claim 2 , and the niobium dioxide and the zirconia are present in a tetragonal phase.4. The composite catalyst of claim 1 , wherein the composite catalyst has an average particle diameter of 1 to 50 μm.5. The composite catalyst of claim 1 , wherein the composite catalyst has a mol ratio of nickel oxide to zirconia of 9.9:0.1 to 4.0:6.0.6. A method for preparing the composite catalyst according to claim 1 , the method comprising:obtaining a precursor mixture solution by dissolving a niobium oxide precursor, a nickel oxide precursor, and a zirconia precursor in an organic solvent;drying the precursor mixture solution; andsintering the dried product.7. The method of claim 6 , wherein the nickel oxide precursor is one or more selected from nickel(II) chloride hydrate claim 6 , nickel(II) acetate tetrahydrate claim 6 , and nickel(II) nitrate hexahydrate.8. The method of claim 6 , wherein the zirconia precursor is zirconium acetate claim 6 , or zirconium(IV) oxynitrate hydrate.9. The method of claim 6 , wherein the niobium oxide precursor is ammonium niobate(V) oxalate hydrate or niobium(V) chloride.10. The method of claim 6 , wherein the organic solvent is one or more selected from methanol claim 6 , 1-propanol claim 6 , and 2-propanol.11. The method of claim 6 , wherein the nickel oxide precursor and the zirconia precursor are mixed at a mol ratio of 10:1 to 8:1.12. The ...

METHOD FOR THE HYDROTHERMAL PREPARATION OF MOLYBDENUM-BISMUTH-COBALT-IRON-BASED MIXED OXIDE CATALYSTS

The present invention relates to a process for preparing molybdenum-bismuth-iron-cobalt-based multielement oxide catalysts by means of hydrothermal synthesis, wherein the hydrothermal synthesis is conducted with an aqueous solution and/or an aqueous suspension of precursor compounds of the elements present in the multielement oxide catalyst to be prepared, the pH of which has been adjusted to a value between about 6 and about 8. The present invention also further relates to the multielement oxide catalysts obtainable by this process and to the use thereof in the partial gas phase oxidation of olefins and tert-butanol. 1. A process for preparing a multielement oxide catalyst , the process comprising:providing a mixture of an aqueous solution and/or an aqueous suspension of precursor compounds of elements present in the multielement oxide catalyst in an amount to achieve stoichiometry thereof,setting a pH of the mixture obtained from the providing to a value between 5.5 and 8.5,reacting the mixture comprising the precursor compounds obtained from the setting under solvothermal reaction conditions in an autoclave at a temperature of from 100° C. to 600° C. to form the multielement oxide catalyst, andseparating the multielement oxide catalyst from the aqueous solution and/or suspension, {'br': None, 'sub': a', 'b', 'c', 'd', 'g', 'f', 'g', 'h', 'i', 'j', 'x, 'MoBiCoFeNiXX′X″X′″X″″O\u2003\u2003(I),'}, 'wherein the multielement oxide catalyst is of formula (I)whereinX is W or P,X′ is Li, K, Na, Rb, Cs, Mg, Ca, Ba or Sr,X″ is Ce, Mn, Cr or V,X″′ is Nb, Se, Te, Sm, Gd, La, Y, Pd, Pt, Ru, Ag or Au,X″″ is Si, Al, Ti or Zr,a is 12,b is 1 to 4,c is 4 to 10,d is 1 to 4,e is 0 to 4,f is 0 to 5,g is 0 to 2,h is 0 to 5,i is 0 to 2,j is 0 to 800, andx is a number which is determined by a valency and frequency of the elements other than oxygen.2. The process according to claim 1 , wherein the precursor compounds in step a) are salts.3. The process according to claim 1 , wherein the ...

PROCESS FOR PREPARING MODIFIED V-TI-P CATALYSTS FOR SYNTHESIS OF 2,3-UNSATURATED CARBOXYLIC ACIDS

The invention relates to a catalyst composition comprising a mixed oxide of vanadium, titanium, and phosphorus modified with alkali metal. The titanium component is derived from a water-soluble, redox-active organo-titanium compound. The catalyst composition is highly effective at facilitating the vapor-phase condensation of formaldehyde with acetic acid to generate acrylic acid, particularly using an industrially relevant aqueous liquid feed. 1. A process for preparing a 2 ,3-unsaturated carboxylic acid , comprising:contacting a formaldehyde source with a carboxylic acid in the presence of a condensation catalyst under vapor-phase condensation conditions to obtain the 2,3-unsaturated carboxylic acid,wherein the condensation catalyst comprises a mixed oxide of vanadium (V), titanium (Ti), phosphorus (P), and alkali metal (M), andwherein the titanium component is derived from an organo-titanium compound, wherein the organo-titanium compound is titanium(IV) bis(ammonium lactate)dihydroxide.2. The process according to claim 1 , wherein the formaldehyde source is formaldehyde claim 1 , 1 claim 1 ,3 claim 1 ,5-trioxane claim 1 , dimethoxymethane claim 1 , or diacetoxymethane and the carboxylic acid is acetic acid or propionic acid.3. The process according to claim 1 , wherein the formaldehyde source is an aqueous solution of formaldehyde claim 1 , 1 claim 1 ,3 claim 1 ,5-trioxane claim 1 , dimethoxymethane claim 1 , or diacetoxymethane and the carboxylic acid is acetic acid or propionic acid.4. The process according to claim 3 , wherein the aqueous solution comprises from 30 to 65 weight percent of formaldehyde.5. The process according to claim 1 , wherein the alkali metal is selected from at least one of lithium claim 1 , sodium claim 1 , potassium claim 1 , rubidium claim 1 , and cesium.6. The process according to claim 1 , wherein the alkali metal comprises potassium.7. The process according to claim 1 , wherein the catalyst composition further comprises a pre-shaped ...

CATALYSTS FOR PETROCHEMICAL CATALYSIS

Metal oxide catalysts comprising various dopants are provided. The catalysts are useful as heterogenous catalysts in a variety of catalytic reactions, for example, the oxidative coupling of methane to C2 hydrocarbons such as ethane and ethylene. Related methods for use and manufacture of the same are also disclosed. 140-. (canceled)41. A catalyst comprising a mixed oxide of a lanthanide and tungsten , wherein the catalyst further comprises a sodium dopant and at least one doping element from groups 2 , 4-15 , lanthanides or combinations thereof , wherein the catalyst comprises a Cselectivity of greater than 50% and a methane conversion of greater than 20% when the catalyst is employed as a heterogeneous catalyst in the oxidative coupling of methane at a temperature of 750° C. or less.42. The catalyst of claim 41 , wherein the lanthanide is Ce claim 41 , Pr claim 41 , Nd claim 41 , La claim 41 , Eu claim 41 , Sm or Yb.43. The catalyst of claim 41 , wherein the at least one doping element is Fe claim 41 , Co claim 41 , Mn claim 41 , Cu claim 41 , Ni claim 41 , Sr claim 41 , Ga claim 41 , Zr claim 41 , Pb claim 41 , Zn claim 41 , Cr claim 41 , Pt claim 41 , Al claim 41 , Nb claim 41 , La claim 41 , Ba claim 41 , Bi claim 41 , Sn claim 41 , In claim 41 , Ru claim 41 , P or combinations thereof.44. A catalyst comprising a rare earth oxide and two or more dopants claim 41 , wherein the catalyst comprises a Cselectivity of greater than 50% and a methane conversion of greater than 20% when the catalyst is employed as a heterogeneous catalyst in the oxidative coupling of methane at a temperature of 750° C. or less claim 41 , and wherein the dopant comprises Eu/Na claim 41 , Sr/Na claim 41 , Na/Zr/Eu/Ca claim 41 , Mg/Na claim 41 , Sr/Sm/Ho/Tm claim 41 , Sr/W claim 41 , Mg/La/K claim 41 , Na/K/Mg/Tm claim 41 , Na/Dy/K claim 41 , Na/La/Dy claim 41 , Na/La/Eu claim 41 , Na/La/Eu/In claim 41 , Na/La/K claim 41 , Na/La/Li/Cs claim 41 , K/La claim 41 , K/La/S claim 41 , K/Na claim ...

Multi-metallic Catalyst System And Use Of The Same In Preparing Upgraded Fuel From Biomass

The present disclosure provides a multi-metallic catalyst system comprising at least one support, and at least one promoter component and an active component comprising at least two metals uniformly dispersed on the support. The present disclosure also provides a process for preparing the multi-metallic catalyst system. Further, the present disclosure provides a process for preparing upgraded fuel from biomass. The process is carried out in two steps. In the first step, a biomass slurry is prepared and is heated in the presence of hydrogen and a multi-metallic catalyst that comprises at least one support, at least one promoter component, and an active component comprising at least two metals to obtain crude biofuel as an intermediate product. The intermediate product obtained in the first step is then cooled and filtered to obtain a filtered intermediate product. In the second step, the filtered intermediate product is hydrogenated in the presence of the multi-metallic catalyst to obtain the upgraded fuel. The fuel obtained from the process of the present disclosure is devoid of heteroatoms such as oxygen, nitrogen and sulfur. 1. A multi-metallic catalyst system comprising:i. at least one alumina support;ii. a promoter component impregnated on said at least one support; wherein said promoter is at least one selected from the group consisting of Niobium (Nb) and Phosphorous (P); andiii. an active component comprising cobalt and molybdenum, being uniformly dispersed on said at least one support.2. The catalyst system as claimed in claim 1 , wherein said catalyst system is characterized by having BET surface area in the range of 165 to 170 m/g claim 1 , pore volume in the range of 0.48 to 0.50 cc/g claim 1 , pore width in the range of 78 to 82 Å claim 1 , and total acidity in the range of 0.810 to 0.812 mmol/g.3. The catalyst system as claimed in claim 1 , wherein said support is in at least one form selected from the group consisting of spheres claim 1 , extrudates ...

Direct Amination of Hydrocarbons

Process for preparing aminated aromatic hydrocarbons that may be substituted comprising the steps of reacting an aromatic hydrocarbon with ammonia in the presence of a catalyst having a crystalline microporous structure wherein the catalyst comprises vanadium aluminophosphate molecular sieve (VAPO) and/or aluminophosphate molecular sieve (AlPO) and wherein the catalyst is preferably impregnated with nickel and/or copper, and wherein the aromatic hydrocarbon may be substituted. 1. A process for preparing aminated aromatic hydrocarbons comprising the steps of reacting an aromatic hydrocarbon with ammonia in the presence of a catalyst having a crystalline microporous structure wherein the catalyst comprises at least one of vanadium aluminophosphate molecular sieve (VAPO) and aluminophosphate molecular sieve (AlPO).2. The process according to claim 1 , wherein the catalyst is impregnated with nickel in an amount such that the nickel content is between 1 and 30 wt % of the catalyst claim 1 , more preferably between 1 and 10 wt % compared to the total weight of the catalyst.3. The process according to claim 1 , wherein the catalyst is impregnated with copper in an amount such that the copper content is between 1 and 30 wt % of the catalyst claim 1 , more preferably between 1 and 10 wt % compared to the total weight of the catalyst.4. The process according to claim 1 , wherein the catalyst is treated by reduction or calcination.5. The process according to claim 4 , wherein in case the catalyst comprises vanadium the catalyst is reduced in the presence of molecular hydrogen.6. The process according to claim 4 , wherein the reduction with molecular hydrogen occurs at a temperature between 100 and 300° C.7. The process according to claims 4 , wherein the reduction with molecular hydrogen occurs during between 50 and 100 minutes.8. The process according to claim 4 , wherein the calcination with air occurs at a temperature between 400 and 700° C.9. The process according to ...

Process for producing unsaturated nitrile

A process for producing unsaturated nitrile, using a fluidized bed reactor and comprising a reaction step of subjecting hydrocarbon to a vapor phase catalytic ammoxidation reaction in the presence of a catalyst to produce the corresponding unsaturated nitrile, wherein when an internal space of the reactor is divided into two spaces of an upper space occupying a space from an upper end of an inlet of a cyclone to an upper end of the internal space and a lower space occupying a space below the upper end of the inlet of the cyclone and ranging to a dispersion plate, a ratio of an existing amount of the catalyst in the upper space to an existing amount of the catalyst in the lower space is 0.05 to 0.45 in the reaction step.

Catalysts for the oxidative dehydrogenation of alkanes

This document relates to oxidative dehydrogenation catalysts that include molybdenum, vanadium, and oxygen.

CATALYST FOR THE OXIDATIVE COUPLING OF METHANE WITH LOW FEED TEMPERATURES

A catalytic material for oxidative coupling of methane includes: a catalyst with the formula ABCO, wherein: A is selected from alkaline earth metals; B and C are selected from rare earth metals, and wherein B and C are different rare earth metals; and the oxide of at least A, B, and C has basic, redox, or both basic and redox properties, and wherein the elements A, B, and C are selected to create a synergistic effect whereby the catalytic material provides an oxygen conversion of greater than or equal to 50% and a C selectivity of greater than or equal to 70%, and wherein the catalyst provides the oxygen conversion and selectivity at a temperature of 797° F. (425° C.) or greater. The catalyst can be used in an oxidative coupling of methane reactor at lower feed temperatures compared to other catalysts. 1. A catalytic material for oxidative coupling of methane comprising:{'sub': a', 'b', 'c', 'x, 'claim-text': A is selected from alkaline earth metals;', 'B and C are selected from rare earth metals, and wherein', 'B and C are different rare earth metals; and', {'sub': '2', 'sup': '+', 'the oxide of at least A, B, and C has basic, redox, or both basic and redox properties, and wherein the elements A, B, and C are selected to create a synergistic effect whereby the catalytic material provides an oxygen conversion of greater than or equal to 50% and a C selectivity of greater than or equal to 70%, and wherein the catalyst provides the oxygen conversion and selectivity at a temperature of 797° F. (425° C.) or greater.'}], 'a catalyst with the formula ABCO, wherein2. The catalytic material according to claim 1 , wherein the catalyst is thermally stable at a temperature of 797° F. (425° C.) or greater.3. The catalytic material according to claim 1 , wherein the catalyst is thermally stable at a temperature in the range of about 797° F. (425° C.) to about 2 claim 1 ,372° F. (1 claim 1 ,300° C.).4. The catalytic material according to claim 1 , wherein the catalyst provides ...

METHODS OF DEGRADING ORGANIC POLLUTANTS AND PREVENTING OR TREATING MICROBE USING Bi2S3-CdS PARTICLES

Methods of synthesizing BiS—CdS particles in the form of spheres as well as properties of these BiS—CdS particles are described. Methods of photocatalytic degradation of organic pollutants employing these BiS—CdS particles and methods of preventing or reducing microbial growth on a surface by applying these BiS—CdS particles in the form of a solution or an antimicrobial product onto the surface are also specified. 1. A method for degrading an organic pollutant , the method comprising:{'sub': 2', '3, 'contacting BiS—CdS particles with an aqueous solution comprising the organic pollutant to form a mixture;'}illuminating the mixture with a light at a wavelength in a range of 200-700 nm for 0.1-6 hours thereby degrading the organic pollutant; [{'sub': 2', '3, 'the BiS—CdS particles comprise bismuth(III) sulfide and cadmium(II) sulfide;'}, {'sub': 2', '3, 'the BiS—CdS particles are in the form of spheres; and'}, 'the organic pollutant is present in the aqueous solution at a concentration of 1-1,000 mg/L relative to a total volume of the aqueous solution., 'wherein2. The method of claim 1 , wherein an atomic ratio of bismuth to cadmium in the BiS—CdS particles is in a range of 0.5:1 to 4:1 claim 1 , and an atomic ratio of sulfur to bismuth in the BiS—CdS particles is in a range of 3:2 to 8:1.3. The method of claim 1 , wherein the BiS—CdS particles are in the form of spheres with an average diameter of 0.3-5 μm.4. The method of claim 1 , wherein the BiS—CdS particles have a BET surface area of 5-25 m/g claim 1 , a pore size of 10-50 nm claim 1 , and a pore volume of 0.02-0.2 cm/g.5. The method of claim 1 , wherein an amount of the BiS—CdS particles in the mixture is in a range of 0.1-10 g/L relative to a total volume of the mixture.6. The method of claim 1 , wherein at least 30% by mole of the organic pollutant is degraded within 2 hours of illuminating.7. The method of claim 1 , wherein the organic pollutant comprises methyl orange claim 1 , methyl green claim 1 , or both ...

A metal complex catalyst, preparation method thereof, and use thereof in preparing d,l-menthol

The present invention discloses a metal complex catalyst, its preparing method and its application in preparing D,L-menthol, the metal complex catalyst includes weight percent elements as follows: 70-85% of Ni, 8-10% of Al, 5-10% of V, and 2-10% of Co. When this metal complex catalyst is applied in preparing D,L-menthol through thymol hydrogenation, it has the characteristics of high reaction activity and quick racemization of chiral compound. Meanwhile, a certain kind of alkali added in isomerization is the key to reducing light constituent byproduct. The whole process comes in good reaction selectivity, simple preparing technology, low production cost, and environment-friendly synthetic route.

Method for Increasing UV Transmittance of Ethylene Glycol

The present invention provides a method for increasing the UV transmittance of ethylene glycol. The method uses an ethylene glycol solution and hydrogen as raw materials, and uses an alloy catalyst comprising nickel, one or more rare-earth elements, tin, and aluminum, the contents thereof in parts by weight being 10-90, 1-5, 1-60, and 5-9, respectively. The method of the present invention uses an inexpensive, stable-in-aqueous-phase, carrier-free alloy as a catalyst, and continuously adds hydrogen to reduce unsaturated impurities in ethylene glycol. In application of the method of the present invention in continuous industrial-scale production, the use of this type of alloy catalyst could be especially significant for the achievement of long-term system stability and control of production costs.

MULTITUBULAR REACTOR FOR LIQUID PHASE ALCOHOL DEHYDROGENATION AND METHOD FOR LIQUID PHASE ALCOHOL DEHYDROGENATION

The invention relates to a multitubular reactor for dehydrogenation of liquid phase alcohol dehydrogenation and a method of liquid phase alcohol dehydrogenation. Most of the alcohol dehydrogenation reaction is endothermic reaction, the reaction temperature is high and the equilibrium conversion rate is low. 110-. (canceled)11. A multitubular reactor for liquid phase alcohol dehydrogenation , comprising:a reactor shell;a plurality of tubes spaced within the reactor shell, wherein the tubes are made of a gas selectively permeable membrane, which is permeable to hydrogen and oxygen but impermeable to liquid molecules, and wherein one end of the tubes is a liquid phase alcohol inlet, and another end of the tubes is a dehydrogenation product outlet;a dehydrogenation catalyst being provided inside the tubes;an oxidation catalyst being provided outside the tubes and in the reactor shell;at least one oxygen membrane tube disposed in the reactor shell, wherein one end of the oxygen membrane tube is an oxygen inlet, and another end of the oxygen membrane tube is closed; andan oxidation product outlet disposed on the reactor shell.12. The multitubular reactor for liquid phase alcohol dehydrogenation of claim 11 , wherein the gas selectively permeable membrane is made of a molecular sieve claim 11 , silica claim 11 , carbon claim 11 , ceramics claim 11 , porous stainless steel or a composite formed by two or more thereof.13. The multitubular reactor for liquid phase alcohol dehydrogenation of claim 11 , wherein the dehydrogenation catalyst is filled in the form of particles within the tubes claim 11 , and the dehydrogenation catalyst comprises:a supported noble metal and a support thereof, wherein the noble metal is Pd, Pt, Ru or Au, and the support is a metal oxide, a molecular sieve, a carbon material or an organic polymer; anda non-noble metal, wherein the non-noble metal is Cu, Zn, Mn, Ni, Co, Cr or V.14. The multitubular reactor for liquid phase alcohol dehydrogenation of ...

Metal oxide catalyst, method for producing same, and apparatus for producing same

A metal oxide catalyst, which has a bulk composition represented by formula (1) below and which is used to produce a conjugated diolefin by an oxidative dehydrogenation reaction between a monoolefin, having 4 or more carbon atoms, and molecular oxygen, wherein standard deviation obtained by dividing a ratio of Bi molar concentration relative to Mo molar concentration at the surface of a catalyst particle by a ratio of the Bi molar concentration relative to the Mo molar concentration in a catalyst bulk is 0.3 or less. Mo 12 Bi p Fe q A a B b C c D d E e F f O x   (1) (In the formula, A is at least one type of element selected from the group consisting of Ni and Co, B is at least one type of element selected from among alkali metal elements, C is at least one type of element selected from the group consisting of Mg, Ca, Sr, Ba, Zn and Mn, D is at least one type of rare earth element, E is at least one type of element selected from the group consisting of Cr, In and Ga, F is at least one type of element selected from the group consisting of Si, Al, Ti and Zr, O is oxygen, p, q, a, b, c, d, e, f and x denote the number of atoms of Bi, Fe, A, B, C, D, E, F and oxygen, respectively, relative to 12 Mo atoms, and are such that 0.1≤p≤5, 0.5≤q≤8, 0≤a≤10, 0.02≤b≤2, 0≤c≤5, 0≤d≤5, 0≤e≤5 and 0≤f≤200, and x is the number of oxygen atoms required to satisfy valency requirement of other elements present.)

AGGLOMERATED ODH CATALYST

Oxidative dehydrogenation catalysts for converting lower paraffins to alkenes such as ethane to ethylene when prepared as an agglomeration, for example extruded with supports comprising slurries of NbO. 127-. (canceled)28. An agglomerated catalyst , wherein the agglomerated catalyst is prepared from at least: [{'br': None, 'sub': 1.0', '0.12-0.49', '0.6-0.16', '0.15-0.20', 'd, 'MoVTeNbO'}, 'wherein d is a number to satisfy the valence of the oxide; and, '10 wt. % to 95 wt. % of a catalyst active phase of the formula{'sub': 2', '5, '5 wt. % to 90 wt. % of NbOhydrate.'}29. The agglomerated catalyst according to claim 28 , further comprising up to 80 wt. % of a non-antagonistic binder.30. The agglomerated catalyst according to claim 29 , wherein the non-antagonistic binder is chosen from oxides of aluminum claim 29 , titanium claim 29 , and zirconium.31. The agglomerated catalyst according to claim 30 , wherein the non-antagonistic binder is present in the amount of 35 wt. % to 65 wt. % based on the weight of the agglomerated catalyst and the agglomerated catalyst has a surface area up to 250 m/g.32. The agglomerated catalyst according to 30 claim 30 , wherein the oxide of aluminum is Boehmite (Al(O)OH).33. The agglomerated catalyst according to claim 30 , wherein the non-antagonistic binder is an oxide of titanium.34. The agglomerated catalyst according to claim 30 , wherein the non-antagonistic binder is an oxide of zirconium.35. The agglomerated catalyst according to claim 28 , having a cumulative surface area less than 10 m/g as measured by BET and comprising less than 35 wt % of a non-antagonistic binder.36. The agglomerated catalyst according to claim 35 , having a cumulative pore volume from 0.020 to 0.20 cm/g.37. The agglomerated catalyst according to claim 35 , having a pore size distribution less than 40% and having a pore width size less than 200 Angstroms.38. The agglomerated catalyst according to claim 35 , having a percent pore area distribution less than ...

Mesoporous composite catalysts containing bismuth silicate and transition metal oxide

Composite catalysts having bismuth silicate(s) (e.g. Bi 2 SiO 5 ) and transition metal oxide(s) (e.g. nickel oxide) impregnated on mesoporous silica supports such as SBA-15, mesoporous silica foam, and silica sol. Methods of making and characterizing the composite catalysts as well as processes for oxidatively dehydrogenating alkanes (e.g. n-butane) and/or alkenes (e.g. 1-butene, 2-butene) to corresponding dienes (e.g. butadiene) employing the composite catalysts are also described.

PROCEDURE TO PREPARE A SUPPORTED TRIMETALLIC CATALYST FOR PRODUCTION OF ULTRA LOW SULFUR DIESEL AND ITS APPLICATION

According to this invention, a Ni—Mo—W trimetallic catalyst supported on porous alumina is obtained that shows very high activity for hydrotreating (HDT) of gasoils, particularly deep hydrodesulfurization (HDS) and hydrodesnitrogenation (HDN) of straight run gasoil in conditions of moderate pressure. 1. A procedure to obtain a supported trimetallic catalytic formulation for the deep hydrodesulfurization of straight run gasoil and for the production of ultra low sulfur diesel (ULSD) , comprising the following steps:a) preparation of solution containing tungsten (solution a), b) preparation of solution containing molybdenum, nickel and phosphorus (solution b), c) preparation of solution containing nickel and EDTA (solution c), d) preparation of solution containing nickel, molybdenum and EDTA (solution d) and e) mixture of solutions (c) and (d); e) drying the catalytic support at a temperature of 100 to 120° C., for 3 to 6 hours, f) impregnation of the solution (a), ageing of the material for 10 to 15 hours, drying at a temperature of 100 to 120° C. for 3 to 5 hours, g) impregnation of the solution (b), ageing of the material for 8 to 10 hours, drying at a temperature of 100 to 120° C. for 4 to 6 hours, h) impregnation of the mixture of the solutions c+d, ageing of the material during 30-40 minutes, no longer aging time is allowed, and drying at a temperature of 60 to 200° C., for 4 to 15 hours, i) wetting of the catalyst with SRGO, j) sulfiding the impregnated catalyst.2. A procedure according to claim 1 , wherein the following solutions are prepared;a) aqueous solution containing a metal of group VIB as tungsten, from ammonium metatungstate in water, until obtaining a completely transparent and crystalline solution;b) acid solution containing a metal of group VIB, such as Mo and a metal of group VIIIB as Ni, dissolved in a phosphoric acid solution;c) solution containing a metal of group VIIIB as Ni, and an organic compound such as ethylenediaminetetraacetic acid ( ...

MIXED METAL OXIDE AMMOXIDATION CATALYSTS

A catalytic composition useful for the conversion of an olefin selected from the group consisting of propylene, isobutylene or mixtures thereof, to acrylonitrile, methacrylonitrile, and mixtures thereof. The catalytic composition comprises a complex of metal oxides comprising rubidium, bismuth, cerium, molybdenum, iron and other promoters, with a desirable composition. 1. A catalytic composition comprising a complex of metal oxides wherein the relative ratios of the listed elements in said catalyst are represented by the following formula:{'br': None, 'sub': m', 'a', 'b', 'c', 'd', 'e', 'f', 'g', 'h', 'n', 'x, 'MoBiFeADEFGCeRbO'} D is at least one element selected from the group consisting of nickel, cobalt, manganese, zinc, magnesium, calcium, strontium, cadmium and barium;', 'E is at least one element selected from the group consisting of chromium, tungsten, boron, aluminum, gallium, indium, phosphorus, arsenic, antimony, vanadium and tellurium;', 'F is at least one element selected from the group consisting of lanthanum, praseodymium, neodymium, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium thulium, ytterbium, lutetium, scandium, yttrium, titanium, zirconium, hafnium, niobium, tantalum, aluminum, gallium, indium, thallium, silicon lead and germanium;', 'G is at least one element selected from the group consisting of silver, gold, ruthenium, rhodium, palladium, osmium, iridium, platinum and mercury; and, 'wherein A is at least one element selected from the group consisting of lithium, sodium, potassium, and cesium; and'} a is greater than 0, but less than or equal to 7,', 'b is 0.1 to 7,', 'c is greater than 0, but less than or equal to 5,', 'd is 0.1 to 12,', 'e is 0 to 5,', 'f is 0 to 5,', 'g is 0 to 0.2,', 'h is 0.01 to 5,', 'm is 10 to 15,', 'n is greater than 0, but less than or equal to 5,', 'x is the number of oxygen atoms required to satisfy the valence requirements of the other component elements present; and, 'a, b, c, d, e, f, g, ...

Catalyst and use of same

A catalyst comprising: a titanium oxide having an anatase-type crystal structure, and having the vertices and the ridge lines, wherein in a single titanium oxide particle, a vertex density per unit surface area is 8.0×10−4 nm−2 or more, and a ridge line density per unit surface area is 5.0×10−2 nm or more, or a ridge line density per unit volume is 8.0×10−3 nm−2 or more. A complex comprising: a material having a porous structure; and said catalyst. A membrane electrode assembly comprising: an anode; cathode; and an electrolyte membrane, wherein the cathode carries said catalyst on at least a surface of the cathode.

Unsupported Metal Substituted Heteropolyacid Catalysts For Dimerization And/Or Oligomerization of Olefins

The present invention relates to unsupported metal (e.g., cesium) substituted heteropolyacid catalyst compositions useful for the production of butene dimers and/or oligomers from a mixed butenes feed, in which, under mild conditions, all isomers of mixed butenes produce highly branched C8 and C8+ olefins, useful as octane enhancers.

METHOD FOR PRODUCING OXIDE CATALYST AND METHOD FOR PRODUCING UNSATURATED NITRILE

A method for producing an oxide catalyst containing Mo, V, Sb, and Nb, the method including: 1. A method for producing an oxide catalyst comprising Mo , V , Sb , and Nb , the method comprising: a sub-step (I) of preparing an aqueous mixed liquid (A) comprising Mo, V, and Sb,', 'a sub-step (II) of adding hydrogen peroxide to the aqueous mixed liquid (A), thereby facilitating oxidation of the aqueous mixed liquid (A) and obtaining an aqueous mixed liquid (A′), and', 'a sub-step (III) of mixing the aqueous mixed liquid (A′) and a Nb raw material liquid (B), thereby obtaining an aqueous mixed liquid (C);, 'a raw material preparation step comprising'}a drying step of drying the aqueous mixed liquid (C), thereby obtaining a dried powder; anda calcination step of calcining the dried powder under an inert gas atmosphere,wherein a time elapsed from addition of the hydrogen peroxide to the aqueous mixed liquid (A) to mixing the Nb raw material liquid (B) therewith is less than 5 minutes andthe aqueous mixed liquid (A′) before being subjected to the sub-step (III) has an oxidation-reduction potential of 150 to 350 mV.2. The method for producing the oxide catalyst according to claim 1 , wherein in the drying step claim 1 , the aqueous mixed liquid (C) has an oxidation-reduction potential of less than 450 mV.3. The method for producing the oxide catalyst according to claim 1 , wherein the oxide catalyst is represented by the following formula (1):{'br': None, 'sub': 1', 'a', 'b', 'c', 'd', 'e', 'n, 'MoVNbSbTZO\u2003\u2003(1)'}wherein T represents at least one element selected from Ti, W, Mn, and Bi; Z represents at least one element selected from La, Ce, Yb, and Y; a, b, c, d, and e represent atomic ratios of respective elements when an atomic ratio of Mo is 1, and are in a range of 0.05≤a≤0.3, 0.01≤b≤0.15, 0.05≤c≤0.3, 0≤d≤0.1, and 0≤e≤0.1 respectively; and n represents a value satisfying a balance of atomic valences.4. The method for producing the oxide catalyst according to ...

METHODS FOR CONVERTING FLUORINATED COMPOUNDS

Methods of converting a fluorinated compound into a fluorinated acyl fluoride or derivative thereof, the method including reacting the fluorinated compound with a catalytic amount of at least one transition metal compound and an oxygen-containing compound to form the fluorinated acyl fluoride or derivative thereof. Compounds formed using such methods are also included, including for example and derivatives thereof, or combinations thereof. 1. A method of converting a fluorinated compound into a fluorinated acyl fluoride , the method comprising:reacting the fluorinated compound with a catalytic amount of at least one transition metal compound selected from the group consisting of an oxide, a spinel compound, an oxoperoxo metal compound, and oxoperoxo metal complex with organic complexing agents, and a combination thereof; and an oxygen-containing compound to form the fluorinated acyl fluoride,wherein the transition metal compound comprises Ti, V, Cr, Mn, Fe, Co, Ni, Zr, Nb, Mo, Ru, Rh, Pd, Hf, Ta, W, Re, Os, Ir, Pt, or combinations thereof: and{'sub': 2', '3', '2, 'wherein the wherein the oxygen-containing compound comprises an oxygen-containing gas comprising oxygen (O), ozone O), nitrous oxide (NO), or combinations thereof.'}2. The method according to claim 1 , wherein the fluorinated compound comprises at least one epoxide group.3. The method according to claim 1 , wherein the fluorinated compound comprises at least one ether group.4. The method according to claim 1 , wherein the fluorinated compound is a fluorinated olefin containing compound.56-. (canceled)7. The method according to claim 1 , wherein the fluorinated compound is a partially fluorinated four carbon chain compound claim 1 , partially fluorinated five carbon chain compound claim 1 , partially fluorinated six carbon chain compound claim 1 , perfluorinated four carbon chain compound claim 1 , perfluorinated five carbon chain ...

REPLACEABLE MODULAR DEVICE FOR HYDROGEN RELEASE

A modular device for generating hydrogen gas from a hydrogen liquid carrier may include a housing; 1. A modular device for generating hydrogen gas from a hydrogen liquid carrier , the modular device comprising:a housing;at least one inlet for receiving the hydrogen liquid carrier;at least one cartridge arranged within the housing, the cartridge comprising at least one first catalyst configured to cause a release of hydrogen gas when exposed to the hydrogen liquid carrier;at least one gas outlet for expelling the hydrogen gas released in the modular device; andat least one liquid outlet for expelling the hydrogen liquid carrier.2. The modular device of claim 1 , wherein the at least one cartridge further includes:a central support structure wherein the at least one catalyst is mounted to the central support structure on one side.3. The modular device of claim 1 , wherein the at least one catalyst includes a plurality of catalysts and at least one cartridge further includes:a central support structure with a first one of the plurality of catalysts attached to a first side of the central support structure, and a second one of the plurality of catalysts attached to a second side of the central support structure.4. The modular device of claim 1 , wherein the at least one cartridge is removable from the housing.5. The modular device of claim 1 , further including:a marginal cartridge disposed on at least one end of the modular device, the marginal cartridge including at least one second catalyst configured to cause a release of hydrogen gas when exposed to the hydrogen liquid carrier.6. The modular device of further comprising a cooling jacket disposed within the modular device claim 1 , wherein the cooling jacket contains a cooling fluid.7. The modular device of wherein the cooling jacket is disposed within the at least one cartridge.8. The modular device of wherein the at least one catalyst is attached to the cooling jacket with a heat transfer medium.9. The modular ...

Catalyst, acrylic acid production method, and catalyst production method

An object of the present invention is to provide a catalyst ensuring that in the case of causing gas-phase catalytic oxidation of an unsaturated aldehyde and an oxygen-containing gas with use of the catalyst to produce a corresponding unsaturated carboxylic acid, the pressure loss can be kept low and an unsaturated carboxylic acid can be produced with high selectivity. The present invention relates to a ring-shaped or columnar catalyst, which is used at the time of producing a corresponding unsaturated carboxylic acid by causing gas-phase catalytic oxidation of an unsaturated aldehyde and an oxygen-containing gas, wherein the outer peripheral edge part is inclined relative to the center line.

MOLYBDENUM-VANADIUM-IRON- AND/OR MOLYBDENUM-VANADIUM-ALUMINIUM-BASED OXIDATIVE DEHYDROGENATION CATALYST MATERIALS

This document relates to oxidative dehydrogenation catalyst materials that include molybdenum, vanadium, oxygen, and iron; oxidative dehydrogenation catalyst materials that include molybdenum, vanadium, oxygen, and aluminum; and oxidative dehydrogenation catalyst materials that include molybdenum, vanadium, oxygen, iron, and aluminum. 1. A catalyst material , comprising:molybdenum;vanadium;oxygen; andiron, a molar ratio of molybdenum to vanadium is from 1:0.25 to 1:0.50;', 'a molar ratio of molybdenum to iron is from 1:0.25 to 1:5.5; and', 'oxygen is present at least in an amount to satisfy the valency of any present metal oxides., 'wherein2. The catalyst material of claim 1 , wherein the molar ratio of molybdenum to vanadium is from 1:0.30 to 1:0.45.34.-. (canceled)5. The catalyst material of claim 1 , wherein the molar ratio of molybdenum to iron is from 1:3 to 1:5.5.615.-. (canceled)16. The catalyst material of claim 1 , wherein the catalyst material has a 35% conversion temperature of from about 300° C. to about 400° C.1718.-. (canceled)19. The catalyst material of claim 1 , wherein the catalyst material has a selectivity to ethylene of from about 65% to 99%.20. (canceled)21. The catalyst material of claim 1 , wherein at least a portion of the iron comprises Fe(III).22. The catalyst material of claim 1 , wherein at least a portion of the iron comprises amorphous iron.23. The catalyst material of claim 1 , wherein at least a portion of the iron comprises at least one member selected from the group consisting of an iron oxide and an iron oxide hydroxide.2427.-. (canceled)28. The catalyst material of claim 1 , wherein at least a first portion of the iron comprises a goethite claim 1 , and at least a second portion of the iron comprises a hematite.2981.-. (canceled)82. A catalyst material claim 1 , comprising:molybdenum;vanadium;oxygen; andaluminum, a molar ratio of molybdenum to vanadium is from 1:0.1 to 1:0.50;', 'a molar ratio of molybdenum to aluminum is from 1: ...

SUPPORTED CATALYST, MONOLITHIC SELECTIVE CATALYTIC REDUCTION (SCR) CATALYST, PREPARATION METHOD THEREFOR, AND METHOD FOR NITROGEN OXIDES REMOVAL

The present invention relates to a catalyst for NOx removal. More specifically, the present invention relates to a supported catalyst, a monolithic selective catalytic reduction (SCR) catalyst, preparation method therefor, and method for NOx removal. 1. A supported catalyst , comprising:a support, andcatalytically active components supported on the support, which comprise vanadium, antimony and at least one further component selected from the group consisting of silicon, aluminum and zirconium.2. The supported catalyst according to claim 1 , wherein the support comprises at least one selected from the group consisting of TiO claim 1 , AlO claim 1 , SiO claim 1 , ZrO claim 1 , CeO claim 1 , zeolite and the combination thereof at any ratio.3. The supported catalyst according to claim 1 , wherein the support consists of TiO claim 1 , or consists of TiOand SiO claim 1 , or consists of TiOand WO claim 1 , or consists of TiO claim 1 , SiOand WO.4. The supported catalyst according to claim 1 , wherein the catalytically active components comprise or consist of vanadium claim 1 , antimony and silicon.5. The supported catalyst according to claim 1 , wherein the catalytically active components consist of vanadium claim 1 , antimony and aluminum.6. The supported catalyst according to claim 1 , wherein the catalytically active components consist of vanadium claim 1 , antimony and zirconium.7. The supported catalyst according to claim 1 , wherein the catalytically active components are in form of oxides of each of them claim 1 , or composite oxides of two or more of them.8. The supported catalyst according to claim 1 , consisting of:{'sub': '2', 'TiO, as the support, and'}vanadium, antimony and silicon, as the catalytically active components.9. The supported catalyst according to claim 1 , wherein based on the total weight of the support and the catalytically active components claim 1 , the support is contained in an amount of 50 to 97.5% by weight.10. The supported catalyst ...

Catalysts For The Production Of Acrylic Acid Or Its Derivatives

Catalysts for dehydrating hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof to acrylic acid, acrylic acid derivatives, or mixtures thereof with high yield and selectivity, short residence time, and without significant conversion to undesired side products, such as, for example, acetaldehyde, propionic acid, and acetic acid, are provided. The catalysts are mixed protonated monophosphates. Methods of preparing the catalysts are also provided.

USE OF VANADATES AS OXIDATION CATALYSTS

Use of a ternary vanadate of formula (I): FeMeIMeIIVOwherein MeI and MeII are different from each other and each stand for an element selected from the group consisting of Y, La, Ce, Pr, Nd, Sm, Er, Gd, Tb, Dy, Ho, Tm, Yb, Lu, Al, Bi and Sb and wherein x=0.05-0.9; y=0.05-0.9; z=0.05-0.9; x+y+z=1, as a catalyst for the oxidation of carbonaceous compounds in combustion engines. 1. A method of catalytically oxidizing carbonaceous compounds from a combustion engine , comprising: {'br': None, 'sub': x', 'y', 'z', '4, 'FeMeIMeIIVO\u2003\u2003(I),'}, 'contacting a catalyst comprising a ternary vanadate of formula (I) with carbonaceous compounds from the combustion enginewherein MeI and MeII are different from each other and each stand for an element selected from the group consisting of Y, La, Ce, Pr, Nd, Sm, Er, Gd, Tb, Dy, Ho, Tm, Yb, Lu, Al, Bi and Sb and whereinx=0.05−0.9y=0.05−0.9z=0.05−0.9x+y+z=1,the catalyst catalysing oxidation of the carbonaceous compounds from the combustion engine.2. The method according to claim 1 , wherein MeI and MeII each stand for an element selected from the group consisting of Y claim 1 , La claim 1 , Ce claim 1 , Pr claim 1 , Er claim 1 , Al claim 1 , Bi.3. The method according to claim 1 , wherein MeI and MeII each stand for an element selected from the group consisting of Ce claim 1 , La claim 1 , Er claim 1 , Al and Bi.4. The method according to claims 1 , wherein MeI and MeII are selected from the group of the following combinations:MeI=La, MeII=Er,MeI=Ce, MeII=AlMeI=Ce, MeII=Bi,MeI=La, MeII=Al,MeI=Er, MeII=Al, andMeI=Bi, MeII=Al.5. The method according to claims 1 , whereinx=0.1-0.8y=0.1-0.8z=0.1-0.8x+y+z=1.6. The method according to claim 5 , whereinx=0.2-0.6y=0.2-0.6z=0.2-0.6x+y+z=1.7. The method according to claim 1 , wherein the ternary vanadate is selected from the group consisting of:{'sub': 0.33', '0.34', '0.33', '4, 'FeCeAlVO,'}{'sub': 0.5', '0.25', '10.25', '4, 'FeCeAlVO,'}{'sub': 0.33', '0.34', '0.33', '4, 'FeCeBiVO,'}{' ...

MESOPOROUS SILICA SUPPORTED CATALYST FOR OXIDATIVE DEHYDROGENATION

Oxidative dehydrogenation catalysts comprising bismuth and nickel oxides impregnated on mesoporous silica supports such as SBA-15 and mesoporous silica foam. Methods of preparing and characterizing the catalysts as well as processes for oxidatively dehydrogenating n-butane to butadiene using the catalysts are also described. The disclosed catalysts demonstrate higher n-butane conversion and butadiene selectivity than catalysts supported by conventional silica. 1: A catalyst , comprising:a mesoporous silica support which is at least one selected from the group consisting of SBA-15 and mesoporous silica foam; anda catalytic material comprising nickel oxide and bismuth oxide impregnated on the mesoporous silica support;wherein the nickel and bismuth atoms of the nickel oxide and the bismuth oxide are present in amounts of 2-30 wt % and 5-40 wt %, each relative to a weight of the mesoporous silica support.2: The catalyst of claim 1 , wherein the mesoporous silica support has a pore volume of 0.2-3 cm/g and a BET surface area of 200-1 claim 1 ,000 m/g.3: The catalyst of claim 1 , wherein the mesoporous silica support is SBA-15.4: The catalyst of claim 1 , wherein 50-99.9 wt % of the bismuth oxide is present as a non-stoichiometric bismuth oxide relative to a total weight of the bismuth oxide.5: The catalyst of claim 4 , wherein the non-stoichiometric bismuth oxide has a formula of BiO claim 4 , in which x ranges from 0.2 to 0.4.6: The catalyst of claim 1 , which has an average pore diameter of 2-20 nm.7: The catalyst of claim 1 , which has a pore volume of 0.2-2 cm/g.8: The catalyst of claim 1 , which has a BET surface area of 200-700 m/g.9: A method of preparing the catalyst of claim 1 , the method comprising:mixing the mesoporous silica support with an aqueous solution comprising a nickel salt and a bismuth salt to form a mixture;drying the mixture to form a dried mass; andcalcining the dried mass in air at a temperature of 300-700° C. thereby producing the catalyst.10 ...

METHOD FOR PREPARING MIXED METAL OXIDE CATALYSTS CONTAINING MOLYBDENUM AND BISMUTH

The present invention relates to a process for producing mixed oxide catalysts on the basis of molybdenum and bismuth oxides in which the precursor compounds of the components of mixed oxide catalysts provided in the form of a solution and/or suspension are subjected to a spray-drying with a specific temperature regime and the spray particles obtained in this way are then calcined to yield a catalytic active mass, and to the mixed oxide catalysts obtainable by this process and to the use of these catalysts in the partial oxidation of olefms, in particular in the partial gas phase oxidation of propene to acrolein and acrylic acid. The spray drying of the precursor compounds containing solution or suspension is performed in concurrent with a gas stream having a specific entrance temperature. Alternatively, when the main gas stream has a higher entrance temperature, an additional colder gas stream can be fed in downstream. The thus obtained mixed oxide catalysts give lower a maximum temperature in the hot spot of catalyst fixed bed when they are used in the partial gas phase oxidation of olefms. 1. A process for producing a mixed oxide catalyst , the process comprisinga) providing a solution and/or suspension of precursor compounds of components of mixed oxide catalyst, wherein the solution and/or suspension contains a precursor compound of bismuth and a precursor compound of molybdenum or a precursor compound of bismuth and molybdenum, and wherein, when the suspension is subjected to spray-drying, a concentration of solids in the suspension is 10 to 50% by weight,b) spray-drying the solution and/or suspension provided in a) in cocurrent together with a gas stream having an entrance temperature into a spray dryer of 160+/−10° C. to 200+/−10° C. and an exit temperature from the spray dryer of 90+/−10° C. to 105+/−10° C., wherein the gas stream has a mean flow velocity in the spray dryer of 2.0+/−0.3 cm/s to 4.5+/−0.3 cm/s, orb′) spray-drying the solution and/or ...

Denitrification catalyst for vessel, using ceramic nanotubes grown on porous metal structure, and preparation method thereof

A denitrification catalyst using ceramic nanotubes grown on a porous metal structure, including: a porous metal structure having a plurality of pores formed between metal supports such that exhaust gas penetrates through the pores in multiple directions; ceramic nanotubes grown on the porous metal structure through anodic oxidation; and an active material uniformly and highly dispersed as a nano-thin film layer on inner and outer surfaces of the ceramic nanotubes through a deposition or supporting process.

Preparation Method of Denitration Catalyst with Wide Operating Temperature Range for Flue Gas

The invention discloses a preparation method and application of a denitration catalyst with wide operating temperature for flue gas, which utilizes an organic vanadium compound as a vanadium precursor, and titanium dioxide powder or titanium tungsten powder as a carrier, and is prepared by mechanical ball milling method and heat treatment to obtain a catalyst, which denitration of fixed source flue gas under wide temperature range. Compared with the existing arts, the present invention includes minor modifications to the traditional vanadium tungsten titanium catalyst system and adopts the mechanical ball milling method, the activity and resistance to sulfur and water poisoning are improved significantly, thus providing a preparation technology of SCR denitration powder catalyst which is green, highly efficient, low cost and simple in operation. Through the interaction of the organic vanadium precursor with the carrier, the vanadium surface atom concentration of the catalyst is higher, the species of polymeric vanadium is more, and the vanadium oxide is more easily reduced, thereby obtaining higher denitrification activity at low temperature. The denitration catalyst of the present invention has relatively higher activity at 200-450° C. while having good resistance to sulfur and water poisoning.

DEHYDROGENATION CATALYST

The present invention relates to a dehydrogenation catalyst in which a platinum-group metal, an assistant metal, and an alkali metal or alkaline earth metal component are supported on a carrier, wherein the molar ratio of platinum to the assistant metal is 0.5 to 1.49, and the catalyst has an acidity amount of 20 to 150 μmol KOH/g catalyst when it is titrated with KOH. The dehydrogenation catalyst according to the present invention may prevent coke formation from increasing rapidly when the hydrogen/hydrocarbon ratio in a dehydrogenation reaction is reduced, thereby increasing the productivity of the process. Accordingly, it makes it possible to operate the process under a condition in which the hydrogen/hydrocarbon ratio in a dehydrogenation reaction is reduced, thereby improving the economy of the process. 1. A dehydrogenation catalyst in which a platinum-group metal , an assistant metal , and an alkali metal or alkaline earth metal component are supported on a carrier , wherein a molar ratio of platinum to the assistant metal is 0.5 to 1.49 , and the catalyst has an acidity amount of 20 to 150 mol KOH/g catalyst when it is titrated with KOH.2. The dehydrogenation catalyst of claim 1 , wherein the catalyst comprises claim 1 , based on the total weight of the catalyst claim 1 , 0.3 to 0.8 wt % of platinum and 0.4 to 0.9 wt % of the alkali metal or alkaline earth metal.3. The dehydrogenation catalyst of claim 1 , wherein the catalyst has a bulk density of 0.55 to 0.9 g/cc.4. The dehydrogenation catalyst of claim 1 , wherein the catalyst has a pill size of 1.2 to 2.5 mm.5. The dehydrogenation catalyst of claim 1 , wherein the carrier comprises both mesopores having an average pore size of 5 to 100 nm and a total pore volume of 0.05 to 2 cm/g and macropores having an average pore size of 0.1 to 20 μm and a total pore volume of 0.05 to 3 cm/g.6. The dehydrogenation catalyst of claim 1 , wherein the alkali metal or alkaline earth metal is one or more selected from the ...

Process for regenerating a deactivated vanadium-titanium-phosphorous catalyst

A process for regenerating a deactivated vanadium-titanium-phosphorous catalyst which has been used in the production of unsaturated carboxylic acid is disclosed. The process comprises contacting the deactivated vanadium-titanium-phosphorous catalyst with a regeneration stream comprising steam as a regeneration agent at a temperature which is the same or similar to that used in the production of the unsaturated carboxylic acid.

METHOD FOR PRODUCING OXIDE CATALYST AND METHOD FOR PRODUCING UNSATURATED NITRILE

A method for producing an oxide catalyst according to the present invention is a method for producing an oxide catalyst containing Mo, V, Sb, and Nb, the method including: 1. A method for producing an oxide catalyst comprising Mo , V , Sb , and Nb , the method comprising:a raw material preparation step of obtaining an aqueous mixed liquid comprising Mo, V, Sb, and Nb;an aging step of subjecting the aqueous mixed liquid to aging at more than 30° C.;a drying step of drying the aqueous mixed liquid, thereby obtaining a dried powder; anda calcination step of calcining the dried powder, thereby obtaining the oxide catalyst, [{'sub': '3', '(I) in the raw material preparation step, the aqueous mixed liquid is prepared by mixing a Nb raw material liquid comprising Nb with a MoVSb raw material liquid comprising Mo, V, and Sb, wherein ammonia is added to at least one of the MoVSb raw material liquid, the Nb raw material liquid, and the aqueous mixed liquid such that a molar ratio in terms of NH/Nb in the aqueous mixed liquid is adjusted to be 0.7 or more, and in the aging step, a temperature of the aqueous mixed liquid is adjusted to more than 50° C.;'}, '(II) in the aging step, a temperature of the aqueous mixed liquid is adjusted to more than 65° C.; and', {'sub': 2', '2, '(III) in the raw material preparation step, the aqueous mixed liquid is prepared by mixing a Nb raw material liquid comprising Nb with a MoVSb raw material liquid comprising Mo, V, and Sb, wherein a molar ratio in terms of HO/Nb in the Nb raw material liquid is adjusted to less than 0.2, and in the aging step, a temperature of the aqueous mixed liquid is adjusted to more than 50° C.'}], 'wherein, in the raw material preparation step and/or the aging step, precipitation of Nb is facilitated by performing at least one operation selected from the group consisting of the following (I) to (III)3. The method for producing the oxide catalyst according to claim 1 , wherein the oxide catalyst comprises 30% by mass ...

AGGLOMERATED ODH CATALYST

Oxidative dehydrogenation catalysts for converting lower paraffins to alkenes such as ethane to ethylene when prepared as an agglomeration, for example extruded with supports chosen from slurries of TiO, ZrOAlO, AlO(OH) and mixtures thereof have a lower temperature at which 25% conversion is obtained. 1. An agglomerated catalyst comprising: [{'br': None, 'sub': 1.0', '0.12-0.49', '0.06-0.16', '0.15-0.20', 'd, 'MoVTeNbO'}, 'as measured by PIXE and wherein d is a number to satisfy the valence of the oxide; and, '10 wt. % to 95 wt. % of a catalyst of the formula{'sub': 2', '2', '3, '5 wt. % to 90 wt. % of a binder chosen from TiO, AlO, AlO(OH), and mixtures thereof.'}2. The agglomerated catalyst of claim 1 , having a cumulative surface area of less than 35 m/g as measured by BET.3. The agglomerated catalyst of claim 1 , having a cumulative pore volume from 0.05 to 0.50 cm/g.4. The agglomerated catalyst of claim 1 , having a pore size distribution with less than 4% having a pore width size less than 150 Angstroms.5. The agglomerated catalyst of claim 1 , wherein the agglomerated catalyst is in the shape of a sphere claim 1 , rod claim 1 , ring claim 1 , or a saddle.6. The agglomerated catalyst of claim 5 , wherein the agglomerated catalyst has an average size from 1.3 mm to 5 mm.7. The agglomerated catalyst of claim 5 , wherein the binder is an acidified binder.8. The agglomerated catalyst of claim 5 , wherein the binder is a base treated binder.9. The agglomerated catalyst of claim 7 , wherein the agglomerated catalyst is in the shape of a rod having an aspect ratio from 1 to 5/1.3 and a crush strength up to 100 N/mm.10. The agglomerated catalyst of claim 8 , wherein the agglomerated catalyst is in the shape of a rod having an aspect ratio from 1 to 5/1.3 and a crush strength up to 100 N/mm.11. The agglomerated catalyst of claim 7 , wherein the agglomerated catalyst is in the shape of a sphere having a crush strength up to 100 N.12. The agglomerated catalyst of claim 8 ...

CATALYST FOR ALKANE OXIDATIVE DEHYDROGENATION AND/OR ALKENE OXIDATION

The invention relates to a process for treating a catalyst for alkane oxidative dehydrogenation and/or alkene oxidation, which catalyst is a mixed metal oxide catalyst containing molybdenum, vanadium and niobium, wherein the process comprises: contacting the catalyst with a gas mixture comprising an inert gas and oxygen (O), wherein the amount of oxygen is of from 10 to less than 10,000 parts per million by volume (ppmv), based on the total volume of the gas mixture, at an elevated temperature. 1. A process for the oxidative dehydrogenation of ethane , comprising contacting ethane with a mixed metal oxide catalyst containing molybdenum , vanadium , tellurium and niobium under dehydrogenation conditions wherein the catalyst is pretreated by: contacting the catalyst with a gas mixture comprising an inert gas and oxygen (O) , wherein the amount of oxygen is from 250 to 10 ,000 parts per million by volume (ppmv) , based on the total volume of the gas mixture , at an elevated temperature.2. (canceled)3. A process according to claim 1 , wherein the temperature is of from 300 to 900° C.4. A process according to claim 1 , wherein the temperature is of from 400 to 800° C.5. A process according to claim 1 , wherein the temperature is of from 500 to 700° C.6. A process according to claim 1 , wherein the temperature is of from 550 to 650° C.7. A process according to claim 1 , wherein the amount of oxygen is of from 400 to 9 claim 1 ,000 parts per million by volume.8. A process according to claim 1 , wherein the amount of oxygen is of from 600 to 8 claim 1 ,500 parts per million by volume.9. A process according to claim 1 , wherein the amount of oxygen is of from 800 to 8 claim 1 ,000 parts per million by volume.10. A process according to claim 1 , wherein the amount of oxygen is of from 900 to 7 claim 1 ,500 parts per million by volume. The present application is a divisional application of U.S. patent application Ser. No. 14/398,508, filed Nov. 3, 2014 which is a National ...

MEHTOD FOR HYDROTHERMAL SYNTHESIS OF THREE DIMENSIONAL Bi4MoO9/TiO2 NANOSTRUCTURE HETEROJUNCTION

A method for hydrothermal synthesis of 3D BiMoO/TiOnanostructure heterojunction includes the following step: adding Bi(NO).5HO into distilled water to form a white turbid liquid, and adding an alkaline solution into the white turbid liquid until a potential of hydrogen value of the white turbid liquid is between 3 and 7, thereby obtaining a suspension A; adding TiOnanospheres into the suspension A to form a mixed suspension C; adding NaMoO.2HO into distilled water to be dissolved to obtaining a NaMoOsolution; adding the NaMoOsolution into the mixed suspension C to form a mixture, and adding an alkaline solution into the mixture until a potential of hydrogen value of the mixture is greater than 7, thereby obtaining a mixed suspension D; transferring the mixed suspension D to a closed vessel for a hydrothermal reaction to obtain a hydrothermal synthesis product; and washing and drying the hydrothermal synthesis product. 1. A method for hydrothermal synthesis of 3D BiMoO/TiOnanostructure heterojunction comprising:{'sub': 3', '3', '2, 'adding Bi(NO).5HO into distilled water and stirring to form a white turbid liquid, and adding an alkaline solution into the white turbid liquid while being continuously stirred until a potential of hydrogen value of the white turbid liquid is in a range of 3 to 7, thereby obtaining a suspension A;'}{'sub': '2', 'adding TiOnanospheres into the suspension A and stirring to form a mixed suspension C;'}{'sub': 2', '4', '2', '2', '4', '2', '2', '4, 'adding NaMoO.2HO into distilled water and stirring until NaMoO.2HO is completely dissolved to obtaining a NaMoOsolution;'}{'sub': 2', '4, 'adding the NaMoOsolution into the mixed suspension C and stirring to form a mixture, and adding an alkaline solution into the mixture while being continuously stirred until a potential of hydrogen value of the mixture is greater than 7, thereby obtaining a mixed suspension D;'}transferring the mixed suspension D to a closed vessel for a hydrothermal reaction to ...

Method for Separating Formic Acid from a Reaction Mixture by Means of Extraction

The invention relates to a method for separating formic acid from a reaction mixture by means of extraction, wherein, in addition to the formic acid, the reaction mixture comprises a polyoxometalate ion of general formula [PMoVO] as a catalyst and a solvent that dissolves the catalyst, wherein 6≤x≤11, 1≤y≤6, x+y=12 and 3 Подробнее

HYDROPROCESSING CATALYSTS AND THEIR PRODUCTION

The precursor of a hydroprocessing catalyst is made by impregnating a metal oxide component comprising at least one metal from Group 6 of the Periodic Table and at least one metal from Groups 8-10 of the Periodic Table with an amide formed from a first organic compound containing at least one amine group, and a second organic compound containing at least one carboxylic acid group. Following impregnation heat treatment follows to form in situ generated unsaturation additional to that in the two organic compounds. The catalyst precursor is sulfided to form an active, sulfide hydroprocessing catalyst. 1. (canceled)2. A method for hydroprocessing a biocomponent feedstock , comprising:exposing a biocomponent feedstock comprising a bio-derived fraction and a mineral oil fraction to a bulk mixed metal catalyst, in the presence of hydrogen under effective deoxygenation conditions, the bulk mixed metal catalyst comprising at least one Group VI metal selected from Mo and W and at least one Group VIII metal selected from Co and Ni; and forming a deoxygenated effluent.3. The method of claim 2 , wherein the bio-derived fraction makes up about 20 wt % of the biocomponent feedstock.4. The method of claim 2 , wherein the bio-derived fraction includes a lipids fraction claim 2 , wherein about 2 wt % to about 40 wt % of lipids in the lipids fraction claim 2 , based on the weight of the bio-derived fraction claim 2 , is sourced from algal sources.5. The method of claim 2 , wherein the deoxygenated effluent is substantially oxygen free.6. The method of claim 2 , wherein the dexoygenation conditions comprise a hydrogen partial pressure of from about 5 barg (0.5 MPag) to about 300 barg (30 MPag) claim 2 , a reaction temperature of from about 392° F. to about 842° F. (200° C. to 450° C.) claim 2 , a liquid hourly space velocity of from about 0.05 hrto about 10 hr claim 2 , and a hydrogen treat gas rate from about 200 scf/B (34 Nm/m) to about 10 claim 2 ,000 scf/B (1685 Nm/m).7. The method ...

METHOD FOR PRODUCING OXIDE CATALYST AND METHOD FOR PRODUCING UNSATURATED NITRILE

The present invention relates to a method for producing an oxide catalyst containing Mo, V, Sb, and Nb, the method including a raw material preparation step of obtaining an aqueous mixed liquid containing Mo, V, Sb, and Nb, an aging step of subjecting the aqueous mixed liquid to aging at more than 30° C., a drying step of drying the aqueous mixed liquid, thereby obtaining a dried powder, and a calcination step of calcining the dried powder, thereby obtaining the oxide catalyst, and a method for producing an unsaturated nitrile or an unsaturated acid by using the catalyst. 1. A method for producing an unsaturated nitrile , the method comprising the steps of:producing an oxide catalyst by following steps of:a raw material preparation step of obtaining an aqueous mixed liquid comprising Mo, V, Sb, and Nb;an aging step of subjecting the aqueous mixed liquid to aging at more than 30° C.;a drying step of drying the aqueous mixed liquid, thereby obtaining a dried powder; anda calcination step of calcining the dried powder, thereby obtaining the oxide catalyst, [{'sub': '3', '(I) in the raw material preparation step, the aqueous mixed liquid is prepared by mixing a Nb raw material liquid comprising Nb with a MoVSb raw material liquid comprising Mo, V, and Sb, wherein ammonia is added to at least one of the MoVSb raw material liquid, the Nb raw material liquid, and the aqueous mixed liquid such that a molar ratio in terms of NH/Nb in the aqueous mixed liquid is adjusted to be 0.7 or more, and in the aging step, a temperature of the aqueous mixed liquid is adjusted to more than 50° C.;'}, '(II) in the aging step, a temperature of the aqueous mixed liquid is adjusted to more than 65° C.; and', {'sub': 2', '7, '(III) in the raw material preparation step, the aqueous mixed liquid is prepared by mixing a Nb raw material liquid comprising Nb with a MoVSb raw material liquid comprising Mo, V, and Sb, wherein a molar ratio in terms of HO/Nb in the Nb raw material liquid is adjusted ...

Oxidative dehydrogenation (odh) of ethane

Processes and associated reaction systems for the oxidative dehydrogenation of ethane are provided. In particular, a process is provided that comprises supplying a feed gas comprising ethane and oxygen to a multitubular fixed-bed reactor and allowing the ethane and oxygen to react in the presence of an oxidative dehydrogenation catalyst to yield a reactor effluent comprising ethylene; and supplying a coolant to an interior shell space of the multitubular fixed-bed reactor in a flow pattern that is co-current with the flow of the feed gas through reactor.

Oxidative dehydrogenation catalyst

Oxidative dehydrogenation catalysts comprising MoVNbTeO having improved consistency of composition and a 25% conversion of ethylene at less than 420° C. and a selectivity to ethylene above 95% are prepared by treating the catalyst precursor with H 2 O 2 in an amount equivalent to 0.30-2.8 mL H 2 O 2 of a 30% solution per gram of catalyst precursor prior to calcining.

CALCINATION PROCESS TO PRODUCE ENHANCED ODH CATALYST

Mixed metal oxide catalysts having an amorphous content of not less than 40 wt. % are prepared by calcining the catalyst precursor fully or partially enclosed by a porous material having a melting temperature greater than 600° C. in an inert container including heating the catalyst precursor at a rate from 0.5 to 10° C. per minute from room temperature to a temperature from 370° C. to 540° C. under a stream of pre heated gas chosen from steam and inert gas and mixtures thereof at a pressure of greater than or equal to 1 psig having a temperature from 300° C. to 540° C. and holding the catalyst precursor at that temperature for at least 2 hours and cooling the catalyst precursor to room temperature. 1. A method to calcine a catalyst precursor of the formula{'br': None, 'sub': 1', '0.1-1', '0.1-1', '0.1-1', '0.1-1', '0.01-0.2', '0.2', 'd, 'MoVVNbNbTeXO'} calcining the catalyst precursor in an inert container with flow passage there through, at a rate from 0.5 to 10° C. per minute from room temperature to a holding temperature from 370° C. to 540° C. under a stream of pre heated gas chosen from steam and inert gas and mixtures thereof at a rate of flow comparable to a flow rate of not less 150 sccm through a 2.54 cm diameter tube, with a length of 152 cm at a pressure of greater than or equal to 1 psig having a temperature from 300° C. to 540° C.;', 'holding the catalyst precursor at the holding temperature for at least 2 hours; and', 'cooling the catalyst precursor to room temperature said catalyst precursor being fully or partially enclosed by a porous material having a melting temperature greater than 600° C., 'where X is chosen from Pd, Sb Ba, Al, W, Ga, Bi, Sn, Cu, Ti, Fe, Co, Ni, Cr, Zr, Ca, oxides thereof and mixtures thereof, and d is a number to satisfy the valence of the catalyst while maintaining an amorphous content of not less than 40 wt. % the method comprising'}2. The method according to claim 1 , wherein the inert container is made from high temperature ...

CATALYST AND METHOD FOR REMOVING NOX FROM COMBUSTION EXHAUST GAS

Provided is a catalyst for removing NOx from a combustion exhaust gas, in particular, a low-NOx combustion exhaust gas, wherein the catalyst has a ratio of a pore volume in a range of not less than 500 Å and not more than 3000 Å in a pore diameter relative to a total pore volume of not less than 15% and not more than 40% and preferably a ratio of a pore volume in a range of not less than 1000 Å in the pore diameter relative to the total pore volume of not less than 10% and not more than 45% in a pore volume distribution in a range of not more than 10Å in the pore diameter, and where SILICA is unlikely to be deposited and even when the amount of SILICA deposited is increased, denitration performance is hardly lowered. 1. A catalyst for removing NOx from a combustion exhaust gas , wherein the catalyst has a ratio of a pore volume in a range of pore diameter of not less than 500 Å and not more than 3000 Å relative to a total pore volume of not less than 15% and not more than 40% in a pore volume distribution in a range of pore diameter of not more than 10Å.2. The catalyst according to claim 1 , wherein the catalyst has a ratio of a pore volume in a range of pore diameter of not less than 40 Å and not more than 3000 Å relative to the total pore volume of not less than 80% in the pore volume distribution in the range of pore diameter of not more than 10Å.3. The catalyst according to claim 1 , wherein the catalyst has a ratio of a pore volume in a range of pore diameter of not less than 40 Å relative to the total pore volume of not less than 90% in the pore volume distribution in the range of pore diameter of not more than 10Å.4. The catalyst according to claim 1 ,{'sup': '5', 'wherein the catalyst has a ratio of a pore volume in a range of pore diameter of not less than 1000 Å relative to the total pore volume of not less than 10% and not more than 45% in the pore volume distribution in the range of pore diameter of not more than 10Å.'}5. The catalyst according to claim ...

PHOTOCATALYST HAVING HIGH VISIBLE-LIGHT ACTIVITY

A photocatalyst according to the present invention has a structure in which the titanium dioxide doped with the transition metals is supported on the support such that a band gap thereof is low and a specific surface area thereof is high, thereby exhibiting an excellent photocatalytic activity even in a visible light region and providing an excellent effect of adsorbing an organic compound and removing the same even under a condition in which light is not emitted. 1. A photocatalyst comprising:titanium dioxide doped with a transition metal; anda support on which the titanium dioxide is supported,wherein the support is a reduced graphene oxide or a polymer matrix having a porous structure.2. The photocatalyst of claim 1 , wherein the transition metal comprises one or more selected from the group consisting of vanadium (V) claim 1 , cobalt (Co) claim 1 , and nickel (Ni).3. The photocatalyst of claim 1 , wherein the photocatalyst has a band gap of 4 eV or less.4. The photocatalyst of claim 1 , wherein the support comprises the polymer matrix claim 1 , andthe photocatalyst comprises 0.1 to 15 parts by weight of the titanium dioxide doped with the transition metal, based on 100 parts by weight of the polymer matrix.5. The photocatalyst of claim 4 , wherein the transition metal is vanadium (V).6. The photocatalyst of claim 4 , wherein an average particle diameter of pores formed in the polymer matrix is in a range of 50 to 500 μm claim 4 , and{'sup': '3', 'an average volume of the pores is in a range of 0.01 to 0.03 cm/g.'}7. The photocatalyst of claim 4 , wherein an average BET specific surface area of the photocatalyst is in a range of 100 to 500 m/g.8. The photocatalyst of claim 4 , wherein the polymer matrix comprises one or more selected from the group consisting of a polyurethane resin claim 4 , a polyester resin claim 4 , and polyamide resin.9. The photocatalyst of claim 1 , wherein the support comprises the reduced graphene oxide claim 1 , andthe photocatalyst ...

Method for Producing Butadiene

A method for producing butadiene comprises a step of obtaining a product gas containing butadiene, by feeding a raw-material gas containing straight-chain butene and an oxygen-containing gas containing molecular oxygen to a reactor and performing oxidative dehydrogenation reaction in the presence of a catalyst, wherein the catalyst comprises a composite oxide containing molybdenum and bismuth, and the concentration of hydrocarbons having 5 or more carbon atoms in the raw-material gas is 0.05 mol % to 7.0 mol %. 1. A method for producing butadiene , comprising:a step of obtaining a product gas containing butadiene, by feeding a raw-material gas containing straight-chain butene and an oxygen-containing gas containing molecular oxygen to a reactor and performing oxidative dehydrogenation reaction in the presence of a catalyst, wherein:the catalyst comprises a composite oxide containing molybdenum and bismuth; anda concentration of hydrocarbons having 5 or more carbon atoms in the raw-material gas is 0.05 mol % to 7:0 mol %.2. The method according to claim 1 , wherein the concentration of hydrocarbons having 5 or more carbon atoms in the raw-material gas is 0.2 mol % to 6.0 mol %.3. The method according to claim 1 , wherein the concentration of the straight-chain butene in the raw-material gas is 60 mol % or more. The present invention relates to a method for producing butadiene.Methods for producing butadiene by oxidative dehydrogenation reaction of straight-chain butene in the presence of a catalyst have been conventionally known (for example, Patent Literature 1 and Patent Literature 2).In a method for producing butadiene, for example, a mixture containing straight-chain butene and butanes obtained by removing butadiene from a C4 fraction such as a C4 fraction produced as by-product by naphtha cracking, or a C4 fraction produced as by-product by fluid catalytic cracking is used as a raw material.Furthermore, as a catalyst for such oxidative dehydrogenation reaction, ...

CLUSTER SUPPORTED CATALYST AND METHOD FOR PRODUCING SAME

An improved cluster-supporting catalyst has heteroatom-removed zeolite particles, and catalyst metal clusters supported within the pores of the heteroatom-removed zeolite particles. A method for producing a cluster-supporting catalyst includes the following steps: providing a dispersion liquid containing a dispersion medium and the heteroatom-removed zeolite particles dispersed in the dispersion medium; and in the dispersion liquid, forming catalyst metal clusters having a positive charge, and supporting the catalyst metal clusters within the pores of the heteroatom-removed zeolite particles through an electrostatic interaction. 1. A cluster-supporting catalyst , comprising heteroatom-removed zeolite particles , and catalyst metal clusters supported within the pores of the heteroatom-removed zeolite particles.2. The cluster-supporting catalyst according to claim 1 , wherein the catalyst metal clusters have a positive charge claim 1 , and are supported on the acid sites within the pores of the heteroatom-removed zeolite particles through an electrostatic interaction.3. The cluster-supporting catalyst according to claim 1 , wherein the heteroatom-removed zeolite particles are aluminum-removed zeolite particles.4. The cluster-supporting catalyst according to claim 1 , wherein the catalyst metal clusters are selected from the group consisting of clusters of platinum claim 1 , palladium claim 1 , rhodium claim 1 , iridium claim 1 , ruthenium claim 1 , silver claim 1 , titanium claim 1 , vanadium claim 1 , chromium claim 1 , manganese claim 1 , iron claim 1 , cobalt claim 1 , nickel claim 1 , copper claim 1 , zinc claim 1 , molybdenum claim 1 , tungsten claim 1 , rhenium claim 1 , silicon and germanium claim 1 , and a combinations thereof.5. The cluster-supporting catalyst according to claim 4 , wherein the catalyst metal clusters are selected from the group consisting of clusters of copper and iron claim 4 , and a combinations thereof.6. The cluster-supporting catalyst ...

CONVERSION OF ALCOHOLS TO HYDROCARBONS USING A DUAL CATALYST SYSTEM COMPRISING BASIC OXIDE ON MIXED OXIDE OR MESOPOROUS CARRIER AND ETCHED METAL LOADED ZEOLITE CATALYST

A method for converting an alcohol to hydrocarbons comprises two serially placed catalysts. The fraction of aromatics is reduced to desired levels. The method comprises: a) contacting the alcohol with a first catalyst on a carrier, said carrier is selected from a mixed oxide and a mesoporous carrier, said first catalyst comprises at least one basic oxide and optionally at least one selected from the group consisting of metals and metal oxides, then b) contacting the resulting mixture from step a) with a second catalyst wherein said second catalyst is an etched metal loaded zeolite catalyst wherein the etched metal loaded zeolite catalyst is manufactured with a method comprising etching with subsequent loading of metal onto the catalyst, wherein the metal is in the form of nanoparticles, and wherein at least two different metals are loaded onto the etched zeolite catalyst. The hydrocarbons are recovered and used for instance for fuel including gasoline, kerosene, diesel, and jet propellant, and jet fuel. Naturally, other uses of hydrocarbons should not be excluded. 1. A method for converting an alcohol to hydrocarbons , said method comprising the steps of:a) contacting the alcohol with a first catalyst on carrier, said carrier is selected from a mixed oxide and a mesoporous carrier, said first catalyst comprises at least one basic oxide and optionally at least one selected from the group consisting of metals and metal oxides,b) contacting the resulting mixture from step a) with a second catalyst wherein said second catalyst is an etched metal loaded zeolite catalyst wherein the etched metal loaded zeolite catalyst is manufactured with a method comprising a step of etching with subsequent loading of metal onto the catalyst, wherein the metal is in the form of nanoparticles, and wherein at least two different metals are loaded onto the etched zeolite catalyst,c) recovering the hydrocarbons resulting from the reaction.2. The method according to claim 1 , wherein the ...

Removable protective coating for the receipt of a dust free catalyst

Method for producing catalyst and method for producing acrylonitrile

A method for producing a catalyst according to the present invention includes: a preparation step of preparing a precursor slurry comprising molybdenum, bismuth, iron, silica, and a carboxylic acid; a drying step of spray-drying the precursor slurry and thereby obtaining a dried particle; and a calcination step of calcining the dried particle, wherein the preparation step comprises: a step (I) of mixing a starting material for silica with the carboxylic acid and thereby preparing a silica-carboxylic acid mixed liquid; and a step (II) of mixing the silica-carboxylic acid mixed liquid, molybdenum, bismuth, and iron.

Catalysts for preparation of butadiene by oxydehydrogenation of butene in fluidized bed reactor and method of preparing same and use of same

The invention relates to a catalyst for preparation of butadiene by oxydehydrogenation of butene in a fluidized bed reactor, a method of preparing the same, and use of the same, wherein a method according to an embodiment of the invention comprises: reacting a metal precursor with an alkaline substance to obtain a slurry containing insoluble compound, followed by filtering and washing the slurry; adding a binder and deionized water, followed by agitation to regulate the solid content of the slurry to 10-50%; subjecting the slurry to spray drying granulation, wherein the temperature at the feed port is controlled between 200-400° C., and the temperature at the discharge port is controlled between 100-160° C., to obtain catalyst microspheres; and drying the catalyst microspheres at 80-200° C. for 1-24 h, and then calcining the catalyst microspheres at 500-900° C. for 4-24 h to obtain a catalyst having a general formula of FeXaYbZcOd, comprising Fe, Mg, Zn, Bi, Mo, Mn, Ni, Co, Ba, Ca, and other metals. The catalyst microspheres prepared according to the exemplary method exhibit high mobility, desirable particle size distribution, extremely high mechanical strength and catalytic activity, and are applicable to industrial production of butadiene by oxydehydrogenation of butene in a fluidized bed. When this catalyst is used to prepare butadiene by oxydehydrogenation of butene, the yield of butadiene is 76-86%, and the selectivity to butadiene is 94-97%.

Catalytic conversion of lactic acid to acrylic acid

Disclosed herein is the catalytic dehydration of lactic acid to acrylic acid, which is characterized by a high conversion of lactic acid, a high selectivity for acrylic acid, a high yield of acrylic acid, and correspondingly low selectivity and molar yields for undesired by-products. This is achieved with a particular class of catalysts defined by a mixture of metal-containing phosphate salts that together provide the catalyst with a very high basicity density and low acidity density. Further, the catalyst is believed to be stable and active for lengthy periods heretofore unseen in the art for such dehydration processes.

Reactor for continuously treating polymeric material

A system for continuously treating recycled polymeric material includes a hopper configured to feed the recycled polymeric material into the system. An extruder can turn the recycled polymeric material in a molten material. In some embodiments, the extruder uses thermal fluids, electric heaters, and/or a separate heater. The molten material is depolymerized in a reactor. In some embodiments, a catalyst is used to aid in depolymerizing the material. In certain embodiments, the catalyst is contained in a permeable container. The depolymerized molten material can then be cooled via a heat exchanger. In some embodiments, multiple reactors are used. In certain embodiments, these reactors are connected in series. In some embodiments, the reactor(s) contain removable static mixer(s) and/or removable annular inserts.

Katalyzátor

Katalis

Reactor for continuously treating polymeric material

A system for continuously treating recycled polymeric material includes a hopper configured to feed the recycled polymeric material into the system. An extruder can turn the recycled polymeric material in a molten material. In some embodiments, the extruder uses thermal fluids, electric heaters, and/or a separate heater. The molten material is depolymerized in a reactor. In some embodiments, a catalyst is used to aid in depolymerizing the material. In certain embodiments, the catalyst is contained in a permeable container. The depolymerized molten material can then be cooled via a heat exchanger. In some embodiments, multiple reactors are used. In certain embodiments, these reactors are connected in series. In some embodiments, the reactor(s) contain removable static mixer(s) and/or removable annular inserts.

Process for producing a catalyst consisting of a support body and a catalytically active oxide mass applied to the surface of the support body

催化氧化方法和共轭二烯的制造方法

本发明的目的在于在使用管式反应器用分子态氧进行气相催化部分氧化时，抑制钼复合氧化物系催化剂的性能劣化。本发明涉及催化氧化方法，该方法包括：使用从反应原料供给口侧依次配置有含有Mo化合物的Mo化合物层及含有Mo复合氧化物催化剂的复合氧化物催化剂层的管式反应器，在440℃且混合气体(空气75体积％及水蒸气25体积％)的流通下，所述Mo化合物的Mo挥发量大于所述Mo复合氧化物催化剂的Mo挥发量。

Method of producing catalyst and method of producing acrylonitrile

FIELD: chemistry. SUBSTANCE: invention relates to a method of producing a catalyst and a method of producing acrylonitrile. Described is a method of producing an ammoxidation catalyst, wherein the catalyst comprises: a metal oxide having a total composition represented by formula (1) below; and silica: Mo 12 Bi a Fe b X c Y d Z e O f (1), where X is at least one element selected from the group consisting of nickel, cobalt, magnesium, calcium, zinc, strontium and barium; Y is at least one element selected from a group consisting of cerium, chromium, lanthanum, neodymium, yttrium, praseodymium, samarium, aluminum, gallium and indium; Z is at least one element selected from a group consisting of potassium, rubidium and cesium; a, b, c, d, e and f denote atomic fraction of each element and satisfy conditions 0.1≤a≤3.0, 0.1≤b≤3.0, 0.1≤c≤10.0, 0.1≤d≤3.0 and 0.01≤e≤2.0, respectively, and f is the number of oxygen atoms required to satisfy the requirements of atomic valences of other elements present in formula (1), wherein the method includes: a step of preparing a precursor suspension containing molybdenum, bismuth, iron, silica and carboxylic acid; spray drying the precursor suspension to obtain dry particles; and a step for burning dried particles, where the preparation step includes: step (I) mixing the starting material of silica with a carboxylic acid and thereby obtaining a mixed liquid of silica-carboxylic acid; and stage (II) of mixing said mixed liquid of silica-carboxylic acid, molybdenum, bismuth and iron. Described also is an ammoxidation catalyst obtained using the method described above. Methods of producing acrylonitrile include a step for preparing an ammoxidation catalyst using the method described above and a reaction step for reacting propylene, molecular oxygen and ammonia in the presence of said catalyst. EFFECT: method of producing a catalyst which provides high output of acrylonitrile. 11 cl, 2 dwg, 4 tbl, 40 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13 ...

Catalytic conversion of hydroxypropionic acid or derivatives thereof into acrylic acid and derivatives thereof

FIELD: chemistry. SUBSTANCE: invention relates to methods of producing acrylic acid, acrylic acid derivatives or mixtures thereof, where, in particular, method includes a step of bringing into contact a flow containing hydroxypropionic acid, hydroxypropionic acid derivatives or mixture thereof, with catalyst containing (a) at least one anion of condensed phosphate, which is selected from a group consisting of formulae (I), (II) and (III), where n is equal to at least 2 and m is at least 1; and (b) at least two different cations, wherein said cations include: (i) at least one univalent cation and (ii) at least one polyvalent cation; catalyst is substantially neutrally charged; additionally molar ratio of phosphorus and said at least two different cations is 0.7-1.7, to obtain acrylic acid, acrylic acid derivatives or mixtures thereof as a result of contact with said catalyst. EFFECT: methods for catalytic dehydration of hydroxypropionic acid, hydroxypropionic acid derivatives or mixtures thereof into acrylic acid, acrylic acid derivatives or mixture thereof are carried out with high output and selectivity and without significant conversion into undesirable by-products, such as acetaldehyde, propionic acid and acetic acid. 35 cl, 4 tbl, 15 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (51) МПК C08F 220/06 (2006.01) C08L 33/02 (2006.01) C07C 57/04 (2006.01) C07C 51/377 (2006.01) C07C 57/065 (2006.01) C07C 57/055 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА B01J 27/18 (2006.01) ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ B01J 27/187 (2006.01) B01J 27/25 (2006.01) B01J 35/10 (2006.01) (12) ОПИСАНИЕ (21)(22) Заявка: (13) 2 586 327 B01J 37/03 C2 (2006.01) ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2014135176/04, 11.04.2013 (24) Дата начала отсчета срока действия патента: 11.04.2013 (73) Патентообладатель(и): ДЗЕ ПРОКТЕР ЭНД ГЭМБЛ КОМПАНИ (US) 11.04.2012 US 61/623,054; 06.02.2013 US 13/760,472 (45) Опубликовано: 10.06.2016 Бюл. № 16 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 28.08.2014 C 2 C 2 (56) Список ...

Method of producing acrylic acid or derivatives thereof

FIELD: chemistry. SUBSTANCE: invention relates to methods of producing acrylic acid, derivatives of acrylic acid or mixtures thereof, where the method, in particular, includes a step at which there is brought into contact a flow containing hydroxypropionic acid, hydroxypropionic acid derivatives or mixtures thereof, with a catalyst containing: a. anion monohydromonophosphate, which is described by formula (I): [HPO 4 ] 2- (I), b. and anions dihydromonophosphate, described by formula (II): [H 2 PO 4 ] - (II), and c. at least two different cations, while the catalyst is neutrally charged; additionally, the molar ratio of the said anion of monohydromonophosphate and the said anion of dihydromonophosphate in the specified catalyst is from 0.1 to 10. EFFECT: methods for catalytic dehydration of hydroxypropionic acid, hydroxypropionic acid derivatives or mixtures thereof into acrylic acid, acrylic acid derivatives or mixture thereof are carried out with high output and selectivity and without significant conversion into undesirable by-products, such as acetaldehyde, propionic acid and acetic acid. 40 cl, 1 tbl, 3 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (51) МПК C07C 57/04 (2006.01) C07C 51/377 (2006.01) C07C 51/48 (2006.01) C07C 51/09 (2006.01) B01J 27/16 (2006.01) B01J 27/188 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА B01J 27/195 (2006.01) ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ B01J 27/198 (2006.01) B01J 27/186 (2006.01) B01J 27/187 (2006.01) (12) ОПИСАНИЕ (24) Дата начала отсчета срока действия патента: 11.04.2013 (72) Автор(ы): ВЕЛАСКЕС Хуан Эстебан (US), ЛИНГОЕС Джанетт Виллалобос (US), КОЛЛИАС Димитрис Иоаннис (US), ГОДЛЕВСКИ Джейн Эллен (US) (73) Патентообладатель(и): ДЗЕ ПРОКТЕР ЭНД ГЭМБЛ КОМПАНИ (US) 61/623,054; 13/760,472; 13/839,986; 13/835,187 (43) Дата публикации заявки: 20.04.2016 Бюл. № 11 (45) Опубликовано: 20.06.2016 Бюл. № 17 C 2 C 2 (56) Список документов, цитированных в отчете о поиске: US 2859240 A, 04.11.1958. WO 03/082795 A2, 09.10.2003. US 4729978 A, 08.03.1988. US ...

Catalyst, method for producing catalyst, method for producing acrylonitrile

본 발명은 몰리브덴과 비스무트와 철을 포함하는 촉매로서, 환원율이 0.20∼5.00％의 범위인 촉매를 제공한다. The present invention provides a catalyst comprising molybdenum, bismuth, and iron, with a reduction rate in the range of 0.20 to 5.00%.

분진 없는 촉매를 제공하기 위한 제거 가능한 보호 피막

본 발명은, 촉매 물질로 형성된 촉매체를 포함하는 안정화된 촉매 금형에 관한 것으로서, 상기 촉매 물질은 촉매 활성 물질 또는 촉매 활성 물질의 전구체 물질을 포함하고, 촉매 금형의 표면의 적어도 일부에 유기 결합제를 포함하는 보호 피막이 제공되어 있음을 특징으로 한다. 또한, 본 발명은, 안정화된 촉매 금형을 수득하기 위한 방법에 관한 것이다.

Catalyst.

Catalysts for conversion of hydroxypropionic acid or derivatives thereof into acrylic acid or derivatives thereof

FIELD: chemistry. SUBSTANCE: catalysts are mixed condensed phosphates, containing (a) at least one anion condensed phosphate of formula (I) [P n O 3n+1 ] (n+2)- (I), where n is equal to at least 2, and (b) at least two different cation. Catalyst, in fact, neutral charge, and molar ratio of phosphorus and said at least two different cations is from 0.7 to 1.7. Cations include: (i) at least one univalent cation; and (ii) at least one polyvalent cation, and the multivalent cation is selected from the group consisting of Be 2+ , Mg 2+ , Ca 2+ , Sr 2+ , Ba 2+ , Mn 2+ , Co 2+ , Ni 2+ , Cu 2+ , Zn 2+ , Cd 2+ , Sn 2+ , Pb 2+ , Ti 3+ , Cr 3+ , Mn 3+ , Al 3+ , Ga 3+ , Y 3+ , In 3+ , Sb 3+ , Bi 3+ , Si 4+ , Ti 4+ , V 4+ , Ge 4+ , Mo 4+ , Pt 4+ , V 5+ , Nb 5+ , Sb 5+ and mixtures thereof. Invention also discloses methods of producing catalysts. First method comprises steps of mixed and heated at least two different compounds containing phosphor, each said compound is described by one of the formulae (IV) and (XV), or any of hydrated forms said formulae M I   y (H 3-y PO 4 ) (IV); M II   v H (4-2v) P 2 O 7 (XV), where M I represents a univalent cation; where M II is a divalent cation; where y denotes 0, 1, 2 or 3; where v is 0, 1 or 2. Second method comprises steps of mixed and heated (a) at least one compound containing phosphorus, at that each said compound is described by one of the formulae (IV)-(VI) and (XV), or any of hydrated forms said formulae M I   y (H 3-y PO 4 ) (IV); M II   y (H 3-y PO 4 ) 2 (V); M III   y (H 3-y PO 4 ) 3 (VI); M II   v H (4-2v) P 2 O 7 (XV), where M I represents a univalent cation; where M II is a divalent cation; where M III is a trivalent cation; where y denotes 0, 1, 2 or 3; where v is 0, 1 or 2; and (b) at least one compound does not contain phosphorus, selected from a group consisting of nitrate salts, at that each said compound is described by one of formulas (XXVI)-(XXVII), or any of hydrated forms said formulae M I NO 3 (XXVI); M II (NO 3 ) ...

Process for preparing hydrotreating catalyst

FIELD: chemistry.SUBSTANCE: invention relates to a method for preparing a hydrotreating catalyst and to a method for hydrotreating a sulfur-containing hydrocarbon feedstock. Said method for preparing a hydrotreating catalyst is that the alumina carrier is impregnated with a solution containing from 14 to up to 40 wt. % of molybdenum, from 2 to up to 12 wt. % of nickel, from 1.5 to 3.5 wt. % of phosphorus and gluconic acid in an amount of from 1 to 60 wt. % relative to the weight of the carrier. If necessary, the treated carrier is dried at a temperature of from 40 to 200 °C. Next, the treated carrier is burned at a temperature of from 200 to 650 °C. Further, the ratio of the weight of gluconic acid to the total weight of nickel and molybdenum, deposited on the carrier, is from 0.7 to 1.5 before firing. Gluconic acid is used in the form of gluconic acid, or a salt of gluconic acid, or a gluconic acid ester. As phosphorus compounds, orthophosphoric acid is used. Said method for hydrotreating a sulfur-containing hydrocarbon feedstock consists in bringing the hydrocarbon feedstock into contact with the above catalyst at a partial pressure of hydrogen of from 1 to 70 bar and a temperature of from 200 to 420 °C.EFFECT: invention allows to obtain a hydrotreating catalyst with high activity.5 cl, 3 tbl, 2 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 678 578 C2 (51) МПК B01J 37/20 (2006.01) B01J 37/00 (2006.01) B01J 37/02 (2006.01) B01J 27/19 (2006.01) B01J 23/883 (2006.01) B01J 37/28 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА B01J 35/10 (2006.01) ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ B01J 35/00 (2006.01) B01J 31/04 (2006.01) C10G 45/08 (2006.01) (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 37/20 (2018.08); B01J 37/086 (2018.08); B01J 37/0201 (2018.08); B01J 27/19 (2018.08); B01J 23/883 (2018.08); B01J 37/28 (2018.08); B01J 35/1019 (2018.08); B01J 35/0006 (2018.08); B01J 31/04 (2018.08); C10G 45/08 (2018.08) 2016120009, 04.11.2014 (24) Дата начала отсчета срока действия патента: 04.11. ...

Method of producing oxide catalyst and method of producing unsaturated nitrile and unsaturated acid

FIELD: chemistry. SUBSTANCE: disclosed is a method of producing an oxide catalyst containing antimony, comprising step (1) dissolving or dispersing a starting material containing an antimony source in a liquid consisting of water and/or a solvent, to produce initial liquid composition using antimony particles containing antimony (III) oxide as said antimony source; step (2) drying said initial liquid material obtained at step (1) to obtain a dried material; stage (3) of roasting said dried material obtained at step (2) to obtain calcined material, where the relative content of pentavalent antimony in the surface layer in the range of up to 2 nm from the surface of antimony particles, measured by X-ray photoelectron spectroscopy (XPS) analysis, is less than 70 at. %, and antimony particles have average particle size of 1.2 mcm or less. Also disclosed is a method of producing an unsaturated nitrile, comprising a step for producing an oxide catalyst which has been obtained using the method described above, and a production step, on which propane or isobutane and NH 3 is subjected to gas-phase catalytic ammoxidation reaction in the presence of obtained oxide catalyst to obtain unsaturated nitrile. Also disclosed is a method of producing an unsaturated acid, comprising a step for producing an oxide catalyst which has been obtained using the method described above, and a production step, at which propane or isobutane is subjected to gas-phase catalytic oxidation reaction in the presence of obtained oxide catalyst to obtain unsaturated acid. Invention discloses use of antimony particles containing antimony (III) oxide as an antimony source in an oxide catalyst to obtain an antimony-containing oxide catalyst, wherein the content of pentavalent antimony in the surface layer in the range of up to 2 nm from the surface of antimony particles, measured by X-ray photoelectron spectroscopy (XPS) analysis, is less than 70 at. %, and said antimony particles have an average particle ...

Способ изготовления катализатора гидроочистки

А 2016119985 ко РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) Я < р _ (11) ОД - За ь 03) (51) МПК ВО1Л 37/20 (2006.01) 777 р у. _. 2 д 5. ре р: ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2016119985, 04.11.2014 (71) Заявитель(и): ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ Приоритет(ы): МААТСХАППИЙ БВ. (№. (30) Конвенционный приоритет: 07.11.2013 ЕР 13191902.9 (72) Автор(ы): (43) Дата публикации заявки: 12.12.2017 Бюл. № 35 АН ИСя Аренд (МГ. (85) Дата начала рассмотрения заявки РСТ на РИГУТТО Марчелло Стефано (МТ.), национальной фазе: 07.06.2016 ГИЛТАЙ Патрисия Йоханна Анне Мария (МГ), (86) Заявка РСТ: ВАН ВЛАНДЕРЕН Йоханнес Якобус ЕР 2014/073637 (04.11.2014) Мария (МТ.), АЗГАЙ Али (МТ.) (87) Публикация заявки РСТ: УГО 2015/067583 (14.05.2015) Адрес для переписки: 129090, Москва, ул. Б.Спасская, 25, строение 3, ООО "Юридическая фирма Городисский и Партнеры" (54) СПОСОБ ИЗГОТОВЛЕНИЯ КАТАЛИЗАТОРА ГИДРООЧИСТКИ (57) Формула изобретения 1. Способ изготовления катализатора гидроочистки, содержащего от 5% вес. до 50% вес. молибдена, от 0,5% вес. до 20% вес. кобальта и от 0 до 5% вес. фосфора относительно общего сухого веса катализатора, включающий: (а) обработку содержащей никель подложки молибденом и кобальтом и от 1 до 60% вес. глюконовой кислоты относительно веса подложки, и, необязательно, фосфором, (5) необязательную сушку обработанной подложки при температуре от 40 до 200°С И (с) обжиг обработанной и, необязательно, высушенной подложки при температуре от 200 до 650°С с получением обожженной обработанной подложки. 2. Способ по п.1, в котором количество глюконовой кислоты составляет от 2 до 40% вес. относительно общего сухого веса подложки. 3. Способ по п.1 или 2, в котором количество фосфора составляет от 1,5 до 3,5% вес. относительно общего сухого веса катализатора. 4. Способ по любому из пп.1-3, в котором подложка представляет собой оксид алюминия. 5. Способ по любому из предшествующих пунктов, в котором катализатор гидроочистки состоит из от 1% вес. до ...

Dehydrogenation catalyst

The present invention relates to a dehydrogenation catalyst, in which a platinum group metal, auxiliary metal, alkali metal or alkali earth metal component is supported on a support, wherein a molar ratio of platinum with respect to the auxiliary metal is 0.5 to 1.49 and, when titrated with KOH, the catalyst has an acid site content of a catalyst of 20 to 150 μmol KOH/g. The dehydrogenation catalyst according to the present invention prevents a phenomenon of a rapid increase of coke in the case of a decline in a hydrogen ratio in a dehydrogenation reaction. Therefore, it is possible to enhance the output of a process to enable operation thereof under a condition of decline in a hydrogen/hydrocarbon ratio, thereby being able to enhance process economics.

ニオブおよびテルルの低下した含有量ならびにエタンの酸化的脱水素化に対するより高い活性を有するＭｏＶＮｂＴｅ触媒の合成

本発明は、元素モリブデン、バナジウム、ニオブおよびテルルを含み、ＸＲＤにおいて、Ｃｕ−Ｋα線を使用した際、回折反射ｈ、ｉ、ｋおよびｌを有し、それらのピークがおよそ回折角（２θ）２６．２°±０．５°（ｈ）、２７．０°±０．５°（ｉ）、７．８°±０．５°（ｋ）および２８．０°±０．５°（ｌ）に位置する、混合酸化物材料であって、以下の化学量論比：Ｍｏ１ＶａＮｂｂＴｅｃＯｎ（Ｉ）（式中、ａ＝０．２〜０．３５、ｂ＝０超０．０８まで、ｃ＝０超０．０８まで、ｎ＝（Ｉ）中の酸素ではない元素の原子価および存在量によって定まる数）を有することを特徴とする、混合酸化物材料に関する。

Catalysts for producing acrylic acid or derivatives thereof

FIELD: chemistry. SUBSTANCE: there are presented catalysts for dehydration of 3-hydroxypropionic acid, derivatives 3-hydroxypropionic acid or mixtures thereof into acrylic acid, acrylic acid derivatives or their mixture with high output and selectivity, short time of stay, and without significant conversion in undesirable by-products, such as, for example, acetaldehyde, propionic acid and acetic acid. Catalyst contains mono-phosphate salt described by formula (III): and mono-phosphate salt described by formula (IV): where M I represents univalent cation and M II is divalent cation, wherein catalyst, in fact, is neutral charged and molar ratio of said M II HPO 4 and said M I H 2 PO 4 in above catalyst is from 0.2 to 5. Method of producing said catalyst includes step where mixed compounds containing phosphor, wherein above compounds contain compound of formula (VI), wherein mentioned a is equal to 1, and compound of formula (VII), where specified a equal to 2: where M I represents univalent cation, where M II is divalent cation. Another method of producing catalyst includes step on which are BaHPO 4 and KH 2 PO 4 are combined in molar ratio of 3:2 to 2:3 to form solid mixture and ground said solid mixture to produce said catalyst. EFFECT: dehydration 3-hydroxypropionic acid, derivatives 3-hydroxypropionic acid or mixtures thereof into acrylic acid, acrylic acid derivatives or their mixture with high output and selectivity. 12 cl, 1 tbl, 3 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) (24) Дата начала отсчета срока действия патента: 11.04.2013 Приоритет(ы): (30) Конвенционный приоритет: US US US US C2 61/623,054; 13/760,444; 13/840,192; 13/835,187 (72) Автор(ы): ВЕЛАСКЕС Хуан Эстебан (US), ЛИНГОЕС Джанетт Виллалобос (US), КОЛЛИАС Димитрис Иоаннис (US), ГОДЛЕВСКИ Джейн Эллен (US), МАМАК Марк Эндрю (US) (73) Патентообладатель(и): ДЗЕ ПРОКТЕР ЭНД ГЭМБЛ КОМПАНИ (US) 2 5 8 6 3 2 9 (43) Дата публикации заявки: 10.04.2016 Бюл. № 10 (45) Опубликовано: 10.06.2016 Бюл. № 16 (85) Дата начала ...

원소 Mo, W, V 및 Cu를 함유하는 촉매 활성 다원소 산화물의 제조 방법

본 발명은, Mo, W, V 및 Cu를 포함하는 촉매 활성 다원소 산화물의 제조 방법에 관한 것으로서, 이때 상기 다원소 산화물의 원소 성분 W의 하나 이상의 공급원으로부터 수용액이 생성되고, 수득된 수용액은 다원소 산화물의 원소 성분 Mo 및 V의 공급원과 혼합되고, 분말(P)는, 수득된 수용액을 건조시켜 생성되고, 기하학적 형상의 전구체 바디는 임의적으로 수득된 분말(P)을 사용하여 생성되고, 분말(P) 또는 기하학적 형상의 전구체 바디는 열처리되어 촉매 활성 조성물을 형성하고, 여기서, 건조에 사용된 수용액은 수용액의 총량에 대해 1.6 중량% 내지 5.0 중량%의 W 및 7.2 중량% 내지 26.0 중량%의 Mo를 함유하는 것을 특징으로 한다.

Process for preparing catalyst and process for producing acrylonitrile

본 발명에 따른 촉매의 제조 방법은, 몰리브덴과 비스무트와 철과 실리카와 카르복실산을 포함하는 전구체 슬러리를 조제하는 조제 공정과, 상기 전구체 슬러리를 분무 건조하여 건조 입자를 얻는 건조 공정과, 상기 건조 입자를 소성하는 소성 공정을 가지며, 상기 조제 공정이, 실리카 원료와 카르복실산을 혼합하여, 실리카-카르복실산 혼합액을 조제하는 공정 (I)과, 상기 실리카-카르복실산 혼합액, 몰리브덴, 비스무트 및 철을 혼합하는 공정 (II)를 포함한다. A method for producing a catalyst according to the present invention includes a preparation step of preparing a precursor slurry containing molybdenum, bismuth, iron, silica, and carboxylic acid, a drying step of spray drying the precursor slurry to obtain dried particles, and the drying It has a baking process which bakes a particle | grain, The said preparation process mixes a silica raw material and carboxylic acid, and prepares a silica-carboxylic-acid mixed liquid, and the said silica-carboxylic acid mixed liquid, molybdenum, bismuth. And step (II) of mixing iron.

Method for producing compound

【課題】反応器に損傷を与えることなく、触媒の飛散を抑制しながら、化合物を高収率で得ることのできる化合物の製造方法を提供することを目的とする。 【解決手段】 触媒が流動可能に収納された内部空間と、流動床反応器に炭化水素を含む原料ガスを供給する第一の供給口と、前記流動床反応器に酸素を含む酸素含有ガスを供給する第二の供給口と、前記流動床反応器から反応生成ガスを排出する排出口と、を有する前記流動床反応器を用い、前記内部空間内で、前記触媒の存在下で前記炭化水素を気相接触酸化反応又は気相接触アンモ酸化反応に供することによりそれぞれ対応する不飽和酸又は不飽和ニトリルを製造する反応工程を有し、該反応工程において、前記第一の供給口における前記原料ガスの線速度（ｍ/ｓｅｃ）を、前記触媒の耐摩耗度（％）に対して、所定の関係を満たすように調整する、化合物の製造方法。 【選択図】なし An object of the present invention is to provide a method for producing a compound capable of obtaining a compound in a high yield while suppressing scattering of a catalyst without damaging a reactor. SOLUTION: An internal space in which a catalyst is flowably housed, a first supply port for supplying a raw material gas containing hydrocarbons to a fluidized bed reactor, and an oxygen-containing gas containing oxygen in the fluidized bed reactor. Using the fluidized bed reactor having a second supply port for supplying and a discharge port for discharging reaction product gas from the fluidized bed reactor, and in the interior space, the hydrocarbon in the presence of the catalyst In the gas phase catalytic oxidation reaction or gas phase catalytic ammoxidation reaction, respectively, to produce a corresponding unsaturated acid or unsaturated nitrile, and in the reaction step, the raw material in the first supply port A method for producing a compound, wherein a linear velocity (m / sec) of a gas is adjusted so as to satisfy a predetermined relationship with a degree of wear resistance (%) of the catalyst. [Selection figure] None

Method of producing an oxide catalyst and a method of producing an unsaturated nitrile

FIELD: chemistry. SUBSTANCE: invention relates to a method of producing an oxide catalyst and a method of producing an unsaturated nitrile. Method of producing oxide catalyst for gas-phase catalytic ammoxidation of propane or isobutane and containing Mo, V, Sb, Nb and silica, includes a step of preparing the starting material, comprising a sub-stage (I) for preparing an aqueous liquid mixture (A) containing Mo, V and Sb; substage (II) for adding hydrogen peroxide to an aqueous liquid mixture (A), thereby promoting oxidation of the aqueous liquid mixture (A) and obtaining an aqueous liquid mixture (A'); and substage (III) mixing aqueous liquid mixture (A'), Nb-containing initial liquid material (B) and initial carrier material containing silica, and thereby obtaining aqueous liquid mixture (C); a step for drying an aqueous liquid mixture (C) and thereby obtaining a dry powder and a step for calcining dry powder in an atmosphere of an inert gas, where time elapsed from adding hydrogen peroxide to the aqueous liquid mixture (A) until mixing with it of an Nb-containing starting liquid material (B) is less than 5 minutes, and aqueous liquid mixture (A') before exposure of substage (III) has oxidation-reduction potential of 150–350 mV. Method of producing acrylonitrile involves a step for producing an oxide catalyst using the above described method of producing an oxide catalyst and a step for producing acrylonitrile, wherein a gas-phase catalytic ammoxidation reaction of propane or isobutane is carried out in the presence of the obtained oxide catalyst to thereby obtain acrylonitrile in accordance therewith. EFFECT: providing a method by which an oxide catalyst which provides high output of an unsaturated nitrile can be obtained without the need to introduce complex steps and modifying agents. 5 cl, 16 ex, 1 tbl РОССИЙСКАЯ ФЕДЕРАЦИЯ ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) (19) RU (11) (13) 2 702 126 C1 (51) МПК B01J 37/04 (2006.01) B01J 37/ ...

羟基丙酸或其衍生物向丙烯酸或其衍生物的催化转化

本发明提供了将羟基丙酸、羟基丙酸衍生物、或它们的混合物催化脱水成丙烯酸、丙烯酸衍生物、或它们的混合物的方法，所述方法具有高收率和选择率，但没有向非期望副产物如乙醛、丙酸和乙酸的显著转化。所述催化剂为混合的缩聚磷酸盐。

Multicomponent oxide catalyst for manufacturing nitrile compounds and its preparing method

본 발명은 다상(multiphase)을 갖는 혼합산화물 촉매와 이의 제조방법에 관한 것으로서, 더욱 상세하게는 서로 다른 조성 및 제조방법에 의해 형성된 코아(core)부분과 쉘(shell)부분의 이중구조를 가지고 있으며 올레핀이나 파라핀 등의 가암모니아 산화반응에 의한 니트릴화합물의 제조시 촉매로 사용되어 우수한 촉매활성을 나타내는 다음 화학식 1로 표시되는 코아-쉘 구조를 가지며 아크릴로니트릴의 수율이 향상된 가암모니아 산화반응용 혼합산화물 촉매와 이의 제조방법에 관한 것이다. The present invention relates to a mixed oxide catalyst having a multiphase and a method for preparing the same, and more particularly, has a dual structure of a core part and a shell part formed by different compositions and methods. Used for the preparation of nitrile compounds by ammonia oxidation reactions such as olefins and paraffins, it has a core-shell structure represented by the following formula (1) which shows excellent catalytic activity and has a high yield of acrylonitrile. It relates to an oxide catalyst and a method for producing the same. [Bi n A a B b Q q R r O x ][(100-z)%Fe f Ni g Mo m O y + z%SiO 2 ] [Bi n A a B b Q q R r O x ] [(100-z)% Fe f Ni g Mo m O y + z% SiO 2 ] 상기 화학식 1에서: A, B, Q, R, m, n, a, q, f, g, z, x 및 y는 각각 발명의 상세한 설명에서 정의한 바와 같다. In Chemical Formula 1, A, B, Q, R, m, n, a, q, f, g, z, x and y are as defined in the detailed description of the invention, respectively.

Catalyst and use of same

Regeneration method of catalyst for butadiene production

Patent RU2019129096A3

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2019 129 096 A (51) МПК B01J 23/887 (2006.01) C07C 11/167 (2006.01) C07C 5/333 (2006.01) C07C 5/48 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2019129096, 16.03.2018 (71) Заявитель(и): МИЦУБИСИ КЕМИКАЛ КОРПОРЕЙШН (JP) Приоритет(ы): (30) Конвенционный приоритет: 17.03.2017 JP 2017-053106 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 17.10.2019 R U (43) Дата публикации заявки: 19.04.2021 Бюл. № 11 (72) Автор(ы): ИВАКАИ, Казуюки (JP), ХИНОИСИ, Хироки (JP), КАМЕО, Хироси (JP), ЯМАГУТИ, Тецуфуми (JP) (86) Заявка PCT: (87) Публикация заявки PCT: WO 2018/169088 (20.09.2018) A Адрес для переписки: 129090, Москва, ул. Б. Спасская, 25, стр. 3, ООО "Юридическая фирма Городисский и Партнеры" R U (57) Формула изобретения 1. Способ каталитического окисления, осуществляющий реакцию каталитического окисления с использованием трубчатого реактора в присутствии молибденового сложнооксидного катализатора, в котором: слой молибденового соединения, содержащий соединение молибдена, и слой сложнооксидного катализатора, содержащий молибденовый сложнооксидный катализатор, расположены в данном порядке со стороны отверстия подачи сырьевого материала трубчатого реактора, и при потоке смешанного газа при температуре 440°С, состоящего из композиции, содержащей 75 об.% воздуха и 25 об.% водяного пара, возгоняемое количество молибдена (мкг/н.л) молибденового соединения оказывается больше, чем возгоняемое количество молибдена (мкг/н.л) молибденового сложнооксидного катализатора. 2. Способ каталитического окисления по п.1, в котором температура слоя молибденового соединения в реакции каталитического окисления равна или ниже температуры реакции. 3. Способ каталитического окисления по п.1 или 2, в котором разница между возгоняемым количеством молибдена молибденового соединения и возгоняемым количеством молибдена молибденового сложнооксидного катализатора составляет 0,2–6 мкг/н.л. Стр ...

Hierarchical porous structure SAPO molecular sieve material and preparation method thereof

本发明涉及一种多级孔结构硅磷铝SAPO分子筛的制备方法，主要解决现有技术难以获得具有多级孔结构SAPO分子筛的问题。本发明通过采用高分子聚合物R1、水、有机模板剂R2、磷源、铝源和碱处理的硅源的混合物在-20℃～100℃条件下水解得到溶胶，然后将其置于反应釜中进行晶化；晶化结束后对样品进行洗涤、干燥和焙烧得到多级孔结构SAPO分子筛的技术方案，较好地解决了该问题，可用于多级孔结构分子筛的工业生产中。

Catalytic conversion of lactic acid into acrylic acid

FIELD: chemistry. SUBSTANCE: in this application described is catalytic dehydration of lactic acid into acrylic acid, characterised by high conversion of lactic acid, high selectivity of producing acrylic acid, high output of acrylic acid and low selectivity of producing and molar outputs of undesirable by-products. Mixed phosphate catalyst for conversion of lactic acid into acrylic acid contains at least two different phosphate salts selected from a group consisting of formulae (I), (II), (III) and (IV): ZH 2 PO 4 (I); X 2-a HPO 4 (II); X 3 (PO 4 ) 2-b (III); X 2+c P 2 O 7 (IV), where Z is a metal group I, and where in each of formulae (II)-(IV) each X independently represents metal group I or II group, with the following conditions: in formula (II), if X is a metal group I, and means 0, and if X is a group II metal, then a denotes 1; in formula (III), if X is a metal group I, b denotes 1, and if X is a group II metal, b denotes 0; and, in the formula (IV), if X is a metal group I, then c means 2, and if X is a group II metal, then c means 0, and additionally said, at least two different phosphate salts contain two metals present in molar ratio relative to each other from 1:9 to 9:1. Also disclosed is a mixed phosphate catalyst containing at least two different phosphate salts, wherein one phosphate salt is a product of deposition of phosphoric acid (H 3 RO 4 ) and nitrate salt of formula (V): X(NO 3 ) 2-b (V), and the other phosphate salt is selected from the phosphate salt of formula (II): X 2-a HPO 4 (II), where in each of formulae (II) and (V) X independently represents metal group I or II group under certain conditions. EFFECT: disclosed is a method of producing acrylic acid by gas-phase catalytic dehydration of lactic acid, the method involves a step on which is brought into contact gaseous mixture containing lactic acid and water, with mixed phosphate catalyst. 17 cl, 1 dwg, 4 tbl, 8 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 598 380 C2 (51) МПК B01J 27/18 ...

Synthesis of MoVNbTe Catalyst with Reduced Niobium and Tellurium Content and Higher Activity for Oxidative Dehydrogenation of Ethane

본 발명은 몰리브덴, 바나듐, 니오븀 및 텔루륨 원소를 포함하는 혼합 산화물 재료로서, Cu-Kα 방사선의 존재하에 XRD에서 회절 반사 h, i, k 및 l를 갖고, 상기 회절 반사가 대략 회절 각 (2θ) 26.2°±0.5°(h), 27.0°±0.5°(i), 7.8°±0.5°(k) 및 28.0°±0.5°(l)에서 피크를 갖고, Mo 1 V a Nb b Te c O n (I) (여기서, a = 0.2 내지 0.35, b = 0 초과 내지 0.08, c = 0 초과 내지 0.08, n = (I)에서 산소 이외의 원소들의 원자가 및 존재비에 의해 결정된 정수)를 특징으로 하는, 혼합 산화물 재료에 관한 것이다. The present invention is a mixed oxide material comprising the elements molybdenum, vanadium, niobium and tellurium, which has diffractive reflections h, i, k and 1 in XRD in the presence of Cu-Kα radiation, wherein the diffraction reflection is approximately at a diffraction angle (2θ) ) with peaks at 26.2°±0.5°(h), 27.0°±0.5°(i), 7.8°±0.5°(k) and 28.0°±0.5°(l), Mo 1 V a Nb b Te c O n (I) (where a = 0.2 to 0.35, b = greater than 0 to 0.08, c = greater than 0 to 0.08, n = an integer determined by the valence and abundance of elements other than oxygen in (I)) , to a mixed oxide material.

Multimetal composited oxide catalyst and process for the preparation of acrylic acid using the same

PURPOSE: Disclosed are a complex metal oxide catalyst composed multiple metal elements and a preparing method of acrylic acid using the same. The catalyst has a composition form, Moa Vb Wc Pbd Cue Xf Yg (MhPMo12-i)jOk and the reaction for preparing acrylic acid is carried out under the reaction condition of low feed ratio of oxygen to acrolein and without a strong basic compound. CONSTITUTION: The complex metal oxide catalyst for preparing acrylic acid has a composition form, Moa Vb Wc Pbd Cue Xf Yg (MhPMo12-i)jOk, where X is one species of La, Ce, Sm, or Tl, Y is one species of Te, Sb, or Nb, M is Ce or Ru, and a, b, c, d, e, f, and g are atomic ratio values of respective elements. When a is 12, b, c, d, e, f, g, h, i, or j are 3-7, 1-6, 0.05-2, 0.5-4, 0.01-1, 0.01-1, 0-2, 0-3, and 0.01-0.2, respectively. And, silica, α-alumina, silicon carbide, or zirconium oxide may be used as a catalytic support. The preparation reaction of acrylic acid is carried out under the condition of temperature of 180-380deg.C, space velocity of 500-7000 h-1, feeding ratio of oxygen to acrolein of 0.5-2. Before the reaction, the catalyst is pre-treated at 200-450deg.C for 0.5-10 h in the mixed gas of acrolein, hydrocarbon such as propylene or methanol, and hydrogen.

改进的氧化脱氢催化剂

通过在煅烧前用相当于每克催化剂前体0.30‑2.8mL 30%H 2 O 2 溶液的量的H 2 O 2 处理催化剂前体，制备包括MoVNbTeO的氧化脱氢催化剂，该催化剂具有改善的组成一致性，在低于420℃的25%乙烯转化率和高于95%生成乙烯的选择性。

Bismuth-molybdenum-iron-phosphorus multi-component metal oxide catalyst, Preparing method thereof and Preparing method of 1,3-butadiene using the same

본 발명은 비스무스-몰리브덴-철-인 금속산화물 촉매와 그의 제조방법 및 이를 이용한 1,3-부타디엔의 제조방법에 관한 것으로서, 더욱 상세하게 설명을 하면, 비스무스-몰리브덴-철-인을 특정 몰비로 포함하는 비스무스-몰리브덴-철-인 금속산화물 촉매 및 이의 제조방법에 관한 것이다. 또한, 본 발명은 상기 금속산화물 촉매 하에서, 부텐을 이용하여 1,3-부타디엔을 높은 수율로 제조하는 방법에 관한 것이다. 상기 본 발명의 금속산화물 촉매는 1,3-부타디엔 제조 시 장시간 고 활성을 유지할 수 있는 바, 1.3-부타디엔을 대량 생산할 때, 사용하기에 적합하다. The present invention relates to a bismuth-molybdenum-iron-phosphorus-containing metal oxide catalyst, a process for producing the same, and a process for producing 1,3-butadiene using the catalyst. More particularly, Molybdenum-iron-phosphorus metal oxide catalyst and a process for its preparation. The present invention also relates to a method for producing 1,3-butadiene in high yield by using butene under the metal oxide catalyst. The metal oxide catalyst of the present invention can maintain high activity for a long time in the production of 1,3-butadiene, and is suitable for mass production of 1.3-butadiene.

Mixed catalyst