Method for recovering polyoxoanion compound

A method for recovering a polyoxoanion compound from an aqueous solution containing the polyoxoanion compound which comprises the following steps: Step (1): a step of mixing an organic solvent capable of forming a complex with the above-mentioned polyoxoanion compound with the above-mentioned aqueous solution followed by separating to a first phase containing the above-mentioned polyoxoanion compound and the above-mentioned organic solvent, and a second phase, Step (2): a step of mixing a hydrophobic organic solvent with the above-mentioned first phase followed by separating to an organic phase containing the above-mentioned organic solvent and the above-mentioned hydrophobic organic solvent, and an aqueous phase containing the above-mentioned polyoxoanion compound.

Process for preparing an alkene

A process for the preparation of an alkene from an oxygenate comprising contacting a reactant feedstream comprising at least one oxygenate reactant and water with a supported heteropolyacid catalyst at a temperature of at least 170° C., wherein the process is initiated using a start-up procedure comprising the following steps: (i) heating the supported heteropolyacid catalyst to a temperature of at least 220° C.; (ii) maintaining the heat-treated supported heteropolyacid catalyst of step (i) at a temperature of at least 220° C. for a time sufficient to remove bound water from the heteropolyacid component of the supported heteropolyacid catalyst; and (iii) whilst maintaining the supported heteropolyacid catalyst of step (ii) at a temperature of at least 220° C., contacting the supported heteropolyacid catalyst with the reactant feedstream having a temperature of at least 220° C.

Hydrothermal hydrocatalytic treatment of biomass

A method of hydrothermal hydrocatalytic treating biomass is provided. Lignocellulosic biomass is treated with a digestive solvent to form a pretreated biomass containing soluble carbohydrates. The pretreated biomass is contacted, with hydrogen at a temperature in the range of 150° C. to less than 300° C. in the presence of a pH buffering agent and a supported hydrogenolysis catalyst containing (a) sulfur, (b) Mo or W, and (c) Co, Ni or mixture thereof, incorporated into a suitable support, to form a plurality of oxygenated hydrocarbons.

Method for preparing acrolein from glycerol or glycerine

The invention relates to a method for preparing acrolein from glycerol or glycerin, according to which dehydration of glycerol or glycerin is carried out in the presence of a catalyst which consists in at least one silica modified with zirconium dioxide, titanium dioxide or tungsten trioxide or any combination of these oxides, and a heteropolyacid. This method may be used for making 3-(methylthio)propionic aldehyde (MMP), 2-hydroxy-4-methylthiobutyronitrile (HMBTN), methionine or its analogs, from acrolein.

Porous polymer supported polyoxometalates

A composition for the destruction of chemical warfare agents and toxic industrial chemicals having a polyoxometalate (POM) attached to an amine, carboxylic acid, or ammonium substituted porous polymer. Also disclosed is a method for attaching a POM to an amine, carboxylic acid, or ammonium substituted porous polymer by (1) dissolving the POM in water or an organic solvent, adding the functionalized porous polymer, whereby the POM ionically attaches to the amine, carboxylic acid or ammonium group, or (2) heating the POM and functionalized polymer in the presence of a dehydrating agent whereby an imide bond is produced between the POM and the functionality on the porous polymer.

LOW TEMPERATURE SULFUR TOLERANT TAR REMOVAL WITH CONCOMITANT SYNTHESIS GAS CONDITIONING

A catalyst comprising NiO, a metal mixture comprising at least one of MoO3 or WO3, a mixture comprising at least one of SiOand AlO, and PO. In this embodiment the metal sites on the catalyst are sulfided and the catalyst is capable of removing tar from a synthesis gas while performing methanation and water gas shift reactions at a temperature range from 300° C. to 600° C. 1. A catalyst comprising of:(a) NiO;{'sub': 3', '3, '(b) a metal mixture comprising of at least one of MoOor WO;'}{'sub': 2', '2', '3, '(c) a mixture comprising at least one of: SiOand AlO; and'}{'sub': 2', '5, '(d) PO,'}wherein the metal sites on the catalyst are sulfided and the catalyst is capable of removing tar from a synthesis gas while performing methanation and water gas shift reactions at a temperature range from 300° C. to 600° C.2. The catalyst of claim 1 , wherein the NiO is present from 1 to 10 wt %.3. The catalyst of claim 1 , wherein the metal mixture is present from 10 to 20 wt %.4. The catalyst of claim 1 , wherein the POis present from 0.001 to 1 wt %.5. The catalyst of claim 1 , wherein the synthesis gas is not heated prior to contacting with the catalyst.6. The catalyst of claim 1 , wherein the removal of tar is greater than 65% conversion at 350° C.7. The catalyst of claim 1 , wherein the removal of tar is greater than 70% conversion at 400° C.8. The catalyst of claim 1 , wherein the methanation produces from 150 to 800 μmol/g cat/s of CH.9. The catalyst of claim 1 , wherein the water gas shift produces from 30 to 50% CO conversion.10. A catalyst comprising of:(a) NiO present from 1 to 10 wt %;{'sub': '3', '(b) a metal mixture comprising of MoOfrom 10 to 20 wt %;'}{'sub': 2', '2', '3, '(c) a mixture comprising at least one of: SiOand AlO; and'}{'sub': 2', '5, '(d) POfrom 0.001 to 1 wt %,'}{'sub': '4', 'wherein the metal sites on the catalyst are sulfided and the catalyst is capable of removing tar, with greater than 65% conversion at 350° C., from an unheated synthesis gas ...

HETEROPOLY ACID PROMOTED CATALYST FOR SCR OF NOx WITH AMMONIA

The present invention concerns the selective removal of nitrogen oxides (NOx) from gases. In particular, the invention concerns a process, a highly alkali metal resistant heteropoly acid promoted catalyst and the use of said catalyst for removal of NOx from exhaust or flue gases, said gases comprising alkali or earth alkali metals. Such gases comprise for example flue gases arising from the burning of biomass, combined biomass and fossil fuel, and from waste incineration units. The process comprises the selective catalytic reduction (SCR) of NOx, such as nitrogen dioxide (NO 2 ) and nitrogen oxide (NO) with ammonia (NH 3 ) or a nitrogen containing compound selected from ammonium salts, urea or a urea derivative or a solution thereof as reductant.

CATALYST FOR PRODUCING N-SUBSTITUTED CARBAMATES, AND THE PREPARATION AND APPLICATION OF THE SAME

The present invention relates to a novel catalyst for producing N-substituted carbamates, the preparation of the catalyst and an improved method for producing N-substituted carbamates from these novel catalysts. The active component of the catalyst is a heteropoly acid and the catalyst support comprises a metal oxide or a metalloid oxide. The catalyst can be used to promote the reaction of carbamate and amine, thereby generating N-substituted carbamates with high yield. In the presence of the catalyst, the reaction conditions are relatively mild, the catalytic activity and selectivity of the reaction are high, and the reaction time is relatively short. Furthermore, the catalyst can be conveniently separated from the reaction system and recycled, therefore, the catalyst can be used to facilitate the further scale-up test and commercial application. 112-. (canceled)13. A catalyst for preparing a N-substituted carbamate , wherein the active component of the catalyst comprises a heteropoly acid and the component of the catalyst support comprise a metal oxide or metalloid oxide.14. The catalyst of claim 13 , wherein the heteropoly acid is a Keggin type heteropoly acid.15. The catalyst of claim 14 , wherein the heteropoly acid is selected from the group consisting of HPWO.nHO claim 14 , HPMoO.nHO claim 14 , HSiWO.nHO and HSiMoO.nHO.16. The catalyst of claim 13 , wherein the catalyst support component comprising a metal oxide or a metalloid oxide is selected from the group consisting of zirconium oxide claim 13 , titanium oxide claim 13 , zinc oxide claim 13 , silicon oxide claim 13 , magnesium oxide claim 13 , calcium oxide claim 13 , tin oxide claim 13 , barium oxide claim 13 , cerium oxide claim 13 , lanthanum oxide claim 13 , vanadium pentoxide claim 13 , aluminium oxide and mixtures thereof.17. The catalyst of claim 16 , wherein the metal oxide is selected from the group consisting of a vanadium pentoxide claim 16 , an aluminium oxide and mixtures thereof.18. The ...

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.

PRODUCTION OF ALPHA, OMEGA-DIOLS

Disclosed herein are processes for preparing an α,ω-C-diol, wherein n is 5 or greater, from a feedstock comprising a Coxygenate. In one embodiment, the process comprises contacting the feedstock with hydrogen gas in the presence of a catalyst comprising Cu, a Cu oxide, or mixtures thereof; a heteropoly acid component comprising H[P(WO)], H[Si(WO)], H[P(MoO)], H[Si(MoO)], CsH[P(WO)], CsH[Si(WO)], or mixtures thereof; optionally a second metal component comprising Cr, a Cr oxide, Ni, a Ni oxide, Mn, a Mn oxide, Fe, an Fe oxide, Co, a Co oxide, Mo, a Mo oxide, W, a W oxide, Re, a Re oxide, Zn, or a Zn oxide, Ag, a Ag oxide, SiO, or AlO; optionally at least one promoter comprising Na, K, Mg, Rb, Cs, Ca, Sr, Ba, Ce, or mixtures thereof; and optionally a support. 1. A process for preparing an α ,ω-C-diol , comprising the steps:{'sub': 'n', '(a) providing a feedstock comprising a Coxygenate;'}{'sub': 'n', '(b) contacting the feedstock with hydrogen gas, in the presence of a catalyst and at a temperature and for a time sufficient to form a product mixture comprising an α,ω-C-diol;'}wherein n is 5 or greater; and wherein the catalyst comprises a first metal component, a heteropoly acid component, optionally a second metal component, optionally at least one promoter, and optionally a support;wherein:the first metal component comprises Cu, a Cu oxide, or mixtures thereof;{'sub': 3', '3', '10', '4', '4', '3', '10', '4', '4', '3', '10', '4', '4', '3', '10', '4', '2.5', '0.5', '3', '10', '4', '2.5', '0.5', '3', '10', '4, 'the heteropoly acid component comprises H[P(WO)], H[Si(WO)], H[P(MoO)], H[Si(MoO)], CsH[P(WO)], CsH[Si(WO)], or mixtures thereof;'}{'sub': 2', '2', '3, 'the second metal component comprises Cr, a Cr oxide, Ni, a Ni oxide, Mn, a Mn oxide, Fe, an Fe oxide, Co, a Co oxide, Mo, a Mo oxide, W, a W oxide, Re, a Re oxide, Zn, or a Zn oxide, Ag, a Ag oxide, SiO, or AlO; and'}the promoter comprises Na, K, Mg, Rb, Cs, Ca, Sr, Ba, Ce, or mixtures thereof.2. The process of ...

KEGGIN-TYPE STRUCTURE HETEROPOLY COMPOUND-BASED CATALYST COMPOSITIONS AND THEIR USE IN CONVERSION OF SYNTHESIS GAS TO OXYGENATES

Use a transition metal-containing, Keggin-type heteropoly compound as a catalyst to convert synthesis gas to an alcohol, especially a C-Calcohol. 1. A process for converting synthesis gas to an oxygenate , which process comprises contacting a mixture of hydrogen and carbon monoxide with a catalyst based on a transition metal-containing , Keggin-type heteropoly compound under conditions of temperature , pressure and gas hourly space velocity sufficient to convert said mixture to at least one alcohol wherein the alcohol is a one carbon to six carbon alcohol , the catalyst having a structure represented by general formula M[HPA]MMwhere Mis at least one metal selected from a group consisting of alkali metals , alkaline earth metals , zinc , cobalt , iron , manganese , nickel or copper where sum net charge of Mis equal to net negative charge of HPA anion; HPA is represented by general formula [XMoWTO] wherein Mo is molybdenum , W is tungsten , T is at least one transition metal selected from vanadium , copper , cobalt , iron , titanium , palladium , ruthenium , and manganese , x=0-12 , y=0-3 provided that x+y=0-12 , and X is at least one of phosphorous , silicon , germanium , and cobalt; Mis at least one of rhodium , palladium , iridium , rhenium , ruthenium , platinum and gold , and Mis an optional material that is at least one alkali or alkaline earth metal , provided that when Mis an alkali metal or an alkaline earth metal , it is a different alkali metal or alkaline earth metal than M , when Mis cobalt , X is at least one of phosphorous , silicon and germanium.2. The process of claim 1 , wherein the conditions of temperature claim 1 , pressure and gas hourly space velocity include at least one of a temperature is within a range of from 200° C. to 450° C. claim 1 , a pressure is within a range of from 200 psig (1.38 MPa) to 5 claim 1 ,000 psig (34.47 MPa) claim 1 , and a gas hourly space velocity is within a range of 300 hrto 25 claim 1 ,000 hr.3. The process of claim ...

SPHERICAL MATERIAL BASED ON HETEROPOLYANIONS TRAPPED IN A MESOSTRUCTURED OXIDE MATRIX AND USE THEREOF AS CATALYST IN HYDROCARBON REFINING PROCESSES

Inorganic material having at least two elementary spherical particles, each of said spherical metallic particles: a polyoxometallate with formula (XMOH), where H is hydrogen, O is oxygen, X is phosphorus, silicon, boron, nickel or cobalt and M is one or more vanadium, niobium, tantalum, molybdenum, tungsten, iron, copper, zinc, cobalt and nickel, x is 0, 1, 2 or 4, m is 5, 6, 7, 8, 9, 10, 11, 12 or 18, y is 17 to 72, h is 0 to 12 and q is 1 to 20. 1. An inorganic material constituted by at least two elementary spherical particles , each of said spherical particles comprising metallic particles in the form of a polyoxometallate with formula (XMOH) , where H is a hydrogen atom , O is an oxygen atom , X is an element selected from phosphorus , silicon , boron , nickel and cobalt and M is one or more elements selected from vanadium , niobium , tantalum , molybdenum , tungsten , iron , copper , zinc , cobalt and nickel , x being equal to 0 , 1 , 2 , or 4 , m being equal to 5 , 6 , 7 , 8 , 9 , 10 , 11 , 12 or 18 , y being in the range 17 to 72 , h being in the range 0 to 12 and q being in the range 1 to 20 (y , h and q being whole numbers) , said metallic particles being present within a mesostructured matrix based on an oxide of at least one element Y selected from the group constituted by silicon , aluminium , titanium , tungsten , zirconium , gallium , germanium , tin , antimony , lead , vanadium , iron , manganese , hafnium , niobium , tantalum , yttrium , cerium , gadolinium , europium and neodymium and a mixture of at least two of these elements , said matrix having pores with a diameter in the range 1.5 to 50 nm and having amorphous walls with a thickness in the range 1 to 30 nm , said elementary spherical particles having a maximum diameter of 200 microns.2. A material according to claim 1 , in which said mesostructured matrix is constituted by aluminium oxide claim 1 , silicon oxide or a mixture of silicon oxide and aluminium oxide.3. A material according to ...

CATALYST AND PROCESS FOR PREPARING ACROLEIN AND/OR ACRYLIC ACID BY DEHYDRATION REACTION OF GLYCERIN

A catalyst composition comprising at least an heteropolyacid deposited on a porous titania carrier. 126-. (canceled)27. A process for preparing acrolein by dehydration of glycerin , carried out in the presence of a catalyst , wherein the catalyst composition comprising at least an heteropolyacid in which protons in the hetropolyacid may be partially exchanged by at least one cation selected from elements belonging to Group 1 to Group 16 of the Periodic Table of Elements that have been deposited on a porous titania carrier.29. The process of claim 27 , in which said titania carrier comprises rutile or anatase or amorphous titanium oxide.30. The process of claim 27 , in which said titania earner comprises at least 80% anatase.31. The process of claim 27 , in which said cation is at least one alkali metal cation.32. The process of claim 27 , in which said alkali metal is cesium.33. The process of claim 28 , in which said compound contains at least one element selected from the group comprising W claim 28 , Mo and V.34. A process for preparing acrolein by dehydration of glycerin claim 28 , carried out in the presence of a catalyst claim 28 , wherein the catalyst is prepared according to a method for preparing a catalyst composition comprising impregnating a titania carrier with a solution of at least one metal selected from elements belonging to the Group 1 to Group 16 of the Periodic Table of Elements or onium claim 28 , drying and firing the resulting solid mixture claim 28 , secondly impregnating the resulting solid mixture with a solution of heteropolyacid claim 28 , drying claim 28 , and firing the resulting solid mixture.35. A process for preparing acrolein by dehydration of glycerin claim 28 , carried out in the presence of a catalyst claim 28 , wherein the catalyst is prepared according to a method for preparing a catalyst composition comprising impregnating a titania carrier with a solution of heteropolyacid claim 28 , drying and firing the resulting solid ...

PROCESS FOR MAKING LINEAR LONG-CHAIN ALKANES FROM RENEWABLE FEEDSTOCKS USING CATALYSTS COMPRISING HETEROPOLYACIDS

A hydrodeoxygenation process for producing a linear alkane from a feedstock comprising a saturated or unsaturated Coxygenate that comprises an ester group, carboxylic acid group, carbonyl group and/or alcohol group is disclosed. This process comprises contacting the feedstock with (i) a catalyst comprising about 0.1% to about 10% by weight of a metal selected from Group IB, VIB, or VIII of the Periodic Table, and (ii) a heteropolyacid or heteropolyacid salt, at a temperature between about 150° C. to about 250° C. and a hydrogen gas pressure of at least about 300 psig. By contacting the feedstock with the catalyst and heteropolyacid or heteropolyacid salt under these temperature and pressure conditions, the Coxygenate is hydrodeoxygenated to a linear alkane that has the same carbon chain length as the Coxygenate. 1. A hydrodeoxygenation process for producing a linear alkane from a feedstock comprising a saturated or unsaturated Coxygenate comprising a moiety selected from the group consisting of an ester group , carboxylic acid group , carbonyl group , and alcohol group , wherein the process comprises:{'sub': 10-18', '10-18, 'a) contacting said feedstock with (i) a catalyst comprising about 0.1% to about 10% by weight of a metal selected from Group IB, VIB, or VIII of the Periodic Table, and (ii) a heteropolyacid or heteropolyacid salt, at a temperature between about 150° C. to about 250° C. and a hydrogen gas pressure of at least about 300 psig, wherein the Coxygenate is hydrodeoxygenated to a linear alkane, and wherein the linear alkane has the same carbon chain length as the Coxygenate; and'}b) optionally, recovering the linear alkane produced in step (a).2. The hydrodeoxygenation process of claim 1 , wherein said Coxygenate is a fatty acid or a triglyceride.3. The hydrodeoxygenation process of claim 1 , wherein said feedstock comprises a plant oil or a fatty acid distillate thereof.4. The hydrodeoxygenation process of claim 3 , wherein said feedstock comprises(i) ...

Extruded resid demetallation catalyst

Catalyst supports, supported catalysts, and a method of preparing and using the catalysts for the demetallation of metal-containing heavy oil feedstocks are disclosed. The catalyst supports comprise alumina and 5 wt % or less titania. Catalyst prepared from the supports have at least 30 to 80 volume percent of its pore volume in pores having a diameter of between 200 and 500 angstroms. Catalysts in accordance with the invention exhibit improved catalytic activity and stability to remove metals from heavy feedstocks during a hydroconversion process. The catalysts also exhibit increased sulfur and MCR conversion.

Catalyst, Process For The Preparation Of Said Catalyst And Use Of Said Catalyst In A Process And In A Device For The Preparation Of Olefins

The present invention relates to a catalyst characterized in that it comprises a) at least one metal compound selected from a group consisting of metal carbide, -nitride, -silicide, -phosphide and -sulfide or mixtures thereof, wherein the metal is selected from a group consisting of molybdenum, tungsten, tantalum, vanadium, titanium, niobium, lanthanum and chromium, and b) at least one non-Brønsted-acidic binder selected from a group consisting of AlPO, Bentonite, AlN and NSi. Furthermore, the present invention relates to a process or a device for the preparation of olefins from C2-, C3- or C4-alkanes using the catalyst. 1. A catalyst , characterized in that it comprises:a) at least one metal compound selected from a group consisting of metal carbide, -nitride, -silicide, -phosphide and -sulfide or mixtures thereof, wherein the metal is selected from a group consisting of molybdenum, tungsten, tantalum, vanadium, titanium, niobium, lanthanum and chromium, and{'sub': 4', '4', '3, 'b) 5-40% (w/w) of a non-Brønsted-acidic binder selected from a group consisting of AlPO, Bentonite, AlN and NSi.'}2. The catalyst of claim 1 , characterized in that the component a) is at least one metal compound of the group consisting of MoC claim 1 , MoN claim 1 , MoP claim 1 , MoSi claim 1 , MoS claim 1 , WC claim 1 , WN claim 1 , WP claim 1 , WSi claim 1 , WS claim 1 , TiC claim 1 , TiN claim 1 , TiP claim 1 , TiSi claim 1 , TiS claim 1 , TaC claim 1 , TaN claim 1 , TaP claim 1 , TaSi claim 1 , TaSi claim 1 , TaS claim 1 , VC claim 1 , VN claim 1 , VP claim 1 , VSi claim 1 , VS claim 1 , LaC claim 1 , LaN claim 1 , LaP claim 1 , LaSi claim 1 , LaS claim 1 , NbC claim 1 , NbN claim 1 , NbP claim 1 , NbSi and NbS claim 1 , wherein 0.1 Подробнее

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.

A coordination zirconium phosphotungstate catalyst and its application in catalytic hydrogenation of furfural

The invention discloses a coordination type zirconium phosphotungstate catalyst and its application in catalytic hydrogenation of furfural, belonging to the field of heterogeneous catalysis. The zirconium phosphotungstate catalyst prepared by the invention not only has good catalytic effect on the conversion of furfural to furfuryl alcohol, but also has mild reaction conditions. The yield of solid line furfuryl alcohol can be 98% if it can be reacted for 1 h at 120 ° C., and the amount of catalyst is less, which greatly reduces the energy consumption in the prior art. In addition, the zirconium phosphotungstate prepared by the invention is easy to separate, has good stability for catalyzing the hydrogenation of furfural to furfuryl alcohol, and is a new, efficient and green catalyst. 1. method of making a coordination type zirconium phosphotungstate catalyst comprising: dissolving phosphotungstic acid and ZrClin DMF respectively to obtain phosphotungstic acid solution and ZrClsolution; after ultrasonic treatment , adding phosphotungstic acid solution drop by drop into ZrClsolution within 5-30 min; after uniform mixing , adding triethylamine; then reacting at room temperature for 3-6 hours; aging more than 4 hours; washing for 1-3 times with DMF , methanol , and anhydrous ether respectively; and drying in vacuum at 70-100° C. for more than 8 hours.2. The according to claim 1 , wherein the molar ratio of the phosphotungstate and ZrClis 3:1˜1:3.3. The method according to the concentration of the phosphotungstate solution is (0.05-0.15) mol/L claim 1 , and the concentration of the ZrClsolution is (0.05-0.15) mol/L.4. The method according to the ultrasonic treatment time is 5 to 30 minutes.5. A coordination type zirconium phosphotungstate catalyst prepared by the method according .6. A method for preparing furfuryl alcohol by catalytic hydrogenation of furfural comprising hydrogenating the furfural in presence of the coordination zirconium phosphotungstate of as a ...

Methods for Preparing Diol

Provided is a method for preparing a diol. In the method, a saccharide and hydrogen as raw materials are contacted with a catalyst in water to prepare the diol. The employed catalyst is a composite catalyst comprised of a main catalyst and a cocatalyst, wherein the main catalyst is a water-insoluble acid-resistant alloy; and the cocatalyst is a soluble tungstate and/or soluble tungsten compound. The method uses an acid-resistant, inexpensive and stable alloy needless of a support as a main catalyst, and can guarantee a high yield of the diol in the case where the production cost is relatively low. 1. A method for preparing a diol , characterized by:(a) adding an unsupported main catalyst comprising nickel, one or more rare earth elements, tin and aluminium, and optionally i) tungsten, ii) tungsten and molybdenum, or iii) tungsten, molybdenum and boron or phosphorus to a slurry bed reactor;(b) increasing the reaction system pressure to 5-12 MPa and the reaction temperature to 150-260° C.;(c) adding a soluble tungstic acid salt cocatalyst, hydrogen and a sugar to the slurry bed reactor, wherein the sugar and cocatalyst are fed continuously into the slurry bed reactor in the form of an aqueous sugar solution having a sugar concentration from 20-60 wt % and further comprising the soluble tungstic acid salt cocatalyst to provide gas and a liquid comprising a diol;(d) continuously passing the gas and reaction liquid out of the reactor through a filter to intercept catalyst and(e) separating the diol from the gas and reaction liquid.2. The method for preparing a diol as claimed in claim 1 , characterized in that the diol is ethylene glycol.3. The method for preparing a diol as claimed in claim 2 , characterized in that the reaction system pH is 1-7; more preferably claim 2 , the reaction system pH is 3-6.4. The method for preparing a diol as claimed in claim 1 , characterized in that the sugar is selected from one or more of five-carbon monosaccharides claim 1 , ...

ACID/METAL BIFUNCTIONAL CATALYSTS PRODUCED BY SLURRY METHODS

A method of producing a acid/metal bifunctional catalyst may include: mixing an acid catalyst, a metal catalyst, and a fluid to produce a slurry, wherein the acid catalyst is present at 50 wt % or less relative to a total catalyst weight in the slurry; heating the slurry; producing a powder from the slurry; and calcining the powder to produce the acid/metal bifunctional catalyst. Such acid/metal bifunctional catalyst would be useful in the direct conversion of syngas to dimethyl ether as well as other reactions. 1. A method comprising:mixing an acid catalyst, a metal catalyst, and a fluid to produce a slurry, wherein the acid catalyst is present at 50 wt % or less relative to a total catalyst weight in the slurry;heating the slurry;drying the slurry produce a dried slurry;producing a powder from the dried slurry; andcalcining the powder to produce an acid/metal bifunctional catalyst.2. The method claim 1 , wherein producing the powder from the dried slurry comprises:grinding the dried slurry to produce a powder, wherein the powder comprises 5 wt % or less of the fluid.3. The method of claim 1 , wherein mixing is maintained during heating.4. The method of claim 1 , wherein mixing is performed for 30 minutes to 3 hours.5. The method of claim 1 , wherein heating is to a temperature within 20° C. of a boiling point of the fluid.6. The method of claim 1 , wherein the acid catalyst is selected from the group consisting of a zeolite claim 1 , an ion exchanged zeolite claim 1 , a molecular sieve claim 1 , a metal oxide claim 1 , and any combination thereof.7. The method of claim 1 , wherein the metal catalyst is a M1/M2/Al catalyst claim 1 , wherein M1 is selected from the group consisting of Cu claim 1 , Cr claim 1 , Ag claim 1 , Au claim 1 , Ru claim 1 , Rh claim 1 , Pd claim 1 , Re claim 1 , Os claim 1 , Ir claim 1 , Pt claim 1 , and any combination thereof claim 1 , wherein M2 is selected from the group consisting of Ti claim 1 , V claim 1 , Cr claim 1 , Mn claim 1 , Fe ...

CATALYTIC FORMS AND FORMULATIONS

Catalytic forms and formulations are provided. The catalytic forms and formulations are useful in a variety of catalytic reactions, for example, the oxidative coupling of methane. Related methods for use and manufacture of the same are also disclosed. 1. A catalytic material comprising a plurality of catalytic nanowires in combination with a diluent , wherein the diluent comprises an alkaline earth metal compound , silicon carbide , cordierite , BO , InO , SrAlO , BSrOor combinations thereof , wherein the alkaline earth metal compound is not MgO , CaO , MgAlOor calcium aluminate.2. The catalytic material of claim 1 , wherein the alkaline earth metal compound is MgCO claim 1 , MgSO claim 1 , Mg(PO) claim 1 , CaCO claim 1 , CaSO claim 1 , Ca(PO) claim 1 , CaAlO claim 1 , SrO claim 1 , SrCO claim 1 , SrSO claim 1 , Sr(PO) claim 1 , SrAlO claim 1 , BaO claim 1 , BaCO claim 1 , BaSO claim 1 , Ba(PO) claim 1 , BaAlOor combinations thereof.3. The catalytic material of claim 1 , wherein the alkaline earth metal compound is SrO claim 1 , MgCO claim 1 , CaCO claim 1 , SrCOor combinations thereof.4. The catalytic material of claim 1 , wherein the catalytic material comprises a formed aggregate.5. The catalytic material of claim 4 , wherein the formed aggregate comprises an extrudate6. The catalytic material of claim 4 , wherein the formed aggregate comprises a pressed or cast particle7. The catalytic material of claim 4 , wherein the formed aggregate comprises a monolith8. The catalytic material of claim 1 , wherein the catalytic material is in a shape selected from a cylinder claim 1 , rod claim 1 , star claim 1 , ribbed claim 1 , trilobe claim 1 , disk claim 1 , hollow claim 1 , donut claim 1 , ring-shaped claim 1 , pellet claim 1 , tube claim 1 , spherical claim 1 , honeycomb claim 1 , cup claim 1 , bowl and an irregular shape.9. The catalytic material of claim 1 , wherein the catalytic material is disposed on claim 1 , impregnated in claim 1 , or combinations thereof claim ...

A metal-doped hydroxyapatite catalyst

The present invention provides the use of a metal-doped hydroxyapatite catalyst for highly selective conversion of an alcohol to an aldehyde at low temperatures. More specifically, the invention provides the use of a silver-doped hydroxyapatite catalyst for the highly selective oxidative dehydrogenation of ethanol to acetaldehyde. The present invention also provides the method for converting ethanol to acetaldehyde using a silver-doped hydroxyapatite catalyst.

Halogen-containing compound and use thereof as catalyst ligand in ethylene oligomerization

A halogen-containing compound represented by a formula I and a use thereof as a ligand of an ethylene oligomerization catalyst composition, an ethylene oligomerization catalyst composition comprising the halogen-containing compound, and an ethylene oligomerization method, ethylene trimerization method and ethylene tetramerization method using the catalyst composition. Serving as the ligand of the ethylene oligomerization catalyst, the halogen-containing polymer may effectively improve the catalytic performance of a catalyst system, especially by displaying a significantly improved catalytic performance in an ethylene oligomerization reaction. The maximum catalyst activity may exceed 4×108 g·mol(Cr)−1·h−1, and the total selectivity of 1-hexene and 1-octene exceeds 92 wt %. In a C6 product, the content of 1-hexene may reach about 97%, and in a C8 product, the content of 1-octene may reach more than 98%. The present catalyst composition has good industrial application prospects and economic value.

METAL PHOSPHORUS COMPOUND FOR PREPARING BIODIESEL AND METHOD FOR PREPARING BIODIESEL USING THE SAME

Disclosed is a catalyst including metal phosphide for preparation of biodiesel, and a method of preparing biodiesel from feedstock comprising vegetable oil through hydrotreating using the catalyst. When the catalyst including metal phosphide is used as a catalyst for preparation of biodiesel, preparation activity of hydrotreated biodiesel is high even without continuous supply of sulfiding agent, and hydrotreating and isomerization reactions occur at the same time, thus obtaining high-quality hydrotreated biodiesel having a low pour point. 114.-. (canceled)15. A catalyst for preparation of biodiesel , comprising a metal phosphide as an active component for at least one of hydrotreating or isomerization.16. The catalyst of claim 15 , wherein the metal phosphide is obtained by binding metals selected from the group consisting of a VIB metal claim 15 , a group VIII metal claim 15 , a group VIIB metal and a mixture of a VIB metal claim 15 , a group VIII metal claim 15 , and a group VIIB metal with P.17. The catalyst of claim 16 , wherein the catalyst comprises only the metal phosphide claim 16 , or further comprises as a support or a binder claim 16 , carbon claim 16 , an alkali earth metal oxide claim 16 , an alkali metal oxide claim 16 , alumina claim 16 , silica claim 16 , silica-alumina claim 16 , zirconia claim 16 , titania claim 16 , silicon carbide claim 16 , niobia claim 16 , aluminum phosphate or a mixture thereof.18. The catalyst of claim 16 , further comprising as at least one of a support or a binder claim 16 , an element selected from the group consisting of carbon claim 16 , an alkali earth metal oxide claim 16 , an alkali metal oxide claim 16 , alumina claim 16 , silica claim 16 , silica-alumina claim 16 , zirconia claim 16 , titania claim 16 , silicon carbide claim 16 , niobia claim 16 , aluminum phosphate and a mixture thereof.19. The catalyst of claim 15 , wherein the metal phosphide is obtained by binding a group VIB metal with P and further comprises ...

USE OF CATALYST PREPARED WITH A SUBGROUP VI ELEMENT FOR THE PRODUCTION OF ORGANIC CHEMICALS AND FUELS FROM LIGNIN

A subgroup VI element to prepare a catalyst for the production of organic chemicals and fuels from lignin with the involvement of solvent molecules. The catalytic reaction use a catalyst composed of a molybdenum or tungsten compound as the active phase, with mixing a kind of lignin, a catalyst, and a reactive solvent. An inert or reductive gas such as H2, N2 or Ar is used to purge or fill the reaction vessel. The temperature is above 200° C., the reaction time is sufficient. The liquid product is separated and analyzed; a catalytic process with a very high product yield, up to 90% if calculated accounting the parts from lignin of the product molecules, or up to over 100% if calculated as the mass products. The product includes aromatic compounds, esters, alcohols, monophenols and benzyl alcohols in different ratios according to the composition, the solvent and the other reaction conditions. 1. The characterization of the application of a catalyst prepared with a subgroup VI element for the production of organic chemicals and fuels from lignin is that the lignin , catalyst and solvent were mixed in the sealed reactor. Reductant or inert gas was used to purge the reactor and then the temperature was increased above 200° C. Finally , liquid products were obtained after sufficient reaction time. The solvents employed were deionized water , ethanol or a mixture of water and ethanol with any proportion.2. The characterization of the application of a catalyst prepared with a subgroup VI element for the production of organic chemicals and fuels from lignin in is that the lignin employed includes Kraft lignin claim 1 , alkali lignin claim 1 , Klason lignin claim 1 , enzymatic hydrolysis lignin claim 1 , milled wood lignin and organosolv lignin. The inert gas is nitrogen claim 1 , argon or helium and the reductive gas is hydrogen. The volume fraction of ethanol is 0-100% in the mixture of water and ethanol with any proportion. The liquid products are alcohols claim 1 , esters ...

PRODUCTION OF A CATALYTICALLY ACTIVE, METALLIZED REACTIVE FOAM MATERIAL AND USE THEREOF

The invention relates to a catalytic material which is used as an optofluidic reactor, and also a method for production thereof. In this case, first a reticulated plastic foam can be fabricated which then is coated with at least one first metal or metal alloy layer. Subsequently, a photocatalytic substrate is then applied to the metal or metal alloy layer. The photocatalytic substrate eliminates bacteria, viruses and other harmful substances, as well as fine dust or fungal spores, when the optofluidic reactor is used. 110-. (canceled)12. The method of claim 11 , wherein the metal of the further metal layer is selected from nickel claim 11 , tin claim 11 , silver claim 11 , or alloys thereof.13. A method of producing a catalytic material for eliminating contaminants claim 11 , comprising a base material selected from fluid-permeable reticulated plastic foam claim 11 , metal or a textile base material made of a plastic claim 11 , glass or carbon material claim 11 , wherein the method comprises:(a) coating the base material, if selected from a fluid-permeable reticulated plastic foam or a textile base material made of a plastic, glass or carbon material, with a copper layer of a thickness >1 μm by a vapor deposition or chemical copper deposition;(b) electroplating a copper layer obtained in (a) with copper, iron or aluminum at a layer thickness of more than 10 μm;(c) applying a further metal or metal alloy layer having a thickness >5 μm selected from white bronze, yellow bronze, NiP, Cr, NiCo, ENiCoP, and CoSn and further from Pd, Pt or silver, or alloys thereof with Ni, Zn, Co or Sn; and{'sub': '2', '(d) electroplating or applying by an externally currentless method a photocatalytic TiOmetal-matrix layer having a thickness >1 μm on a metal or metal alloy layer obtained in (c).'}14. The method of claim 13 , wherein the method further comprises (e) applying a layer of bright chrome or a noble metal on a layer obtained in (d).15. The method of claim 13 , wherein the base ...

WATER OXIDATION CATALYSTS AND METHODS OF USE THEREOF

Homogeneous water oxidation catalysts (WOCs) for the oxidation of water to produce hydrogen ions and oxygen, and methods of making and using thereof are described herein. In a preferred embodiment, the WOC is a polyoxometalate WOC which is hydrolytically stable, oxidatively stable, and thermally stable. The WOC oxidized waters in the presence of an oxidant. The oxidant can be generated photochemically, using light, such as sunlight, or electrochemically using a positively biased electrode. The hydrogen ions are subsequently reduced to form hydrogen gas, for example, using a hydrogen evolution catalyst (HEC). The hydrogen gas can be used as a fuel in combustion reactions and/or in hydrogen fuel cells. The catalysts described herein exhibit higher turn over numbers, faster turn over frequencies, and/or higher oxygen yields than prior art catalysts. 1. A method of oxidizing water to oxygen , comprising mixing water with a photosensitizer , and a polyoxometalate water oxidation catalyst , under conditions such that oxygen is formed , wherein the catalyst is [Co(HO)(PWO)][A]wherein A is a cation or combination of cations.2. The method of claim 1 , wherein mixing is done in the presence of an oxidizing agent.3. The method of claim 1 , wherein mixing is done in an electrochemical cell comprising an electrode.4. The method of claim 3 , wherein the electrochemical cell further comprises nanocrystalline TiO.5. The method of claim 1 , wherein the photosensitizer is a ruthenium complex. This Application is a continuation of U.S. application Ser. No. 13/256,227, filed Sep. 13, 2011, now U.S. Pat. No. 8,822,367, issued Sep. 2, 2014, which is a 371 U.S.C of PCT International Patent Serial No. PCT/US2010/027670, filed on Mar. 17, 2010, which claims the benefit of priority to U.S. Provisional Application 61/160,881, filed on Mar. 17, 2009 and U.S. Provisional Application 61/305,301, filed on Feb. 17, 2010. The entirety of each of these applications is incorporated by reference for ...

Catalyst For Preparing Acrolein And Acrylic Acid By Dehydration Of Glycerin, And Its Production Process

An object of the present invention is to provide a catalyst for glycerin dehydration reaction for producing unsaturated aldehyde and unsaturated carboxylic acid at higher yield by a dehydration reaction of glycerin, and that can reduce a decrease in time of the conversion ratio of glycerin and the yields of unsaturated aldehyde and of unsaturated carboxylic acid. Another object of the present invention is to provide a catalyst for glycerin dehydration reaction that can produce acrolein and acrylic acid at higher yield by the dehydration reaction of glycerin, and the catalyst has a longer life. Still another object of the present invention is to provide a method for preparing the catalysts above. A catalyst for glycerin dehydration comprising a carrier, wherein the carrier includes at least one metal oxide selected from the group consisting TiO, SiO, AlO, ZrO, and NbO, wherein the carrier includes a bimodal porous structure in which the volume ratio between a pore volume of mesopores having a pore size of more than 2 nm to less than 50 nm to a pore volume of macropores having a pore size of 50 nm or more is equal to or more than 0.5, and wherein the carrier configures to support a W-containing metal oxide thereon or a metal oxide containing at least one element selected from the group consisting of P, Si, Mo, and V, in addition to the W-containing metal oxide thereon, and to cause a catalytic dehydrogenation reaction with glycerin to produce acrolein and acrylic acid. 1. A catalyst for glycerin dehydration comprising a carrier ,{'sub': 2', '2', '2', '3', '2', '2', '5, 'wherein the carrier includes at least one metal oxide selected from the group consisting TiO, SiO, AlO, ZrO, and NbO,'}wherein the carrier includes a bimodal porous structure in which the volume ratio between a pore volume of mesopores having a pore size of more than 2 nm to less than 50 nm to a pore volume of macropores having a pore size of 50 nm or more is equal to or more than 0.5, andwherein the ...

Purification Of Bio Based Acrylic Acid To Crude And Glacial Acrylic Acid

Processes for the purification of bio-based acrylic acid to crude and glacial acrylic acid are provided. The bio-based acrylic acid is produced from hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof. The purification includes some or all of the following processes: extraction, drying, distillation, and melt crystallization. The produced glacial or crude acrylic acid contains hydroxypropionic, hydroxypropionic acid derivatives, or mixtures thereof as an impurity. 1. A glacial acrylic acid composition wherein a portion of the remaining impurities in said glacial acrylic acid composition is lactic acid; wherein said glacial acrylic acid composition has a bio-based content greater than about 3%; and wherein said glacial acrylic acid composition is produced by the steps comprising:j. Providing an aqueous solution of acrylic acid comprising: 1) acrylic acid; and 2) lactic acid, lactic acid derivatives, or mixtures thereof, and wherein said aqueous solution of acrylic acid is essentially free of maleic anhydride, furfural, and formic acid;k. Extracting said aqueous solution of acrylic acid, with a solvent to produce an extract;l. Drying said extract to produce a dried extract;m. Distilling said dried extract to produce distilled acrylic acid composition;n. Cooling said distilled acrylic acid composition to a temperature from about −21° C. to about 14° C. to produce crystals of acrylic acid;o. Partially melting said crystals of acrylic acid to produce a liquid/solid mixture;p. Decanting said liquid/solid mixture to produce a purified acrylic acid solid composition;q. Fully melting said purified acrylic acid solid composition to produce a purified acrylic acid liquid composition; andr. Determining the acrylic acid purity of said purified acrylic acid liquid composition, and if the purity is less than about 98 wt % acrylic acid, repeating said cooling, partially melting, decanting, and fully melting steps on the purified acrylic acid liquid ...

HYDROPROCESSING OF HYDROCARBON FEEDS WITH A CATALYST COMPRISING AN ALUMINIUM MATERIAL COMPRISING CARBON

The invention relates to a method for hydroprocessing a hydrocarbon feed, operated at a temperature of between 180° C. and 450° C., in the presence of a catalyst comprising i) a composite material comprising a compound based on at least one crystalline aluminium solid and carbon, the deposited carbon content being between 1 and 25 wt. % of the total mass of the composite material, and ii) at least one element of group VIB and at least one element of group VIII, in the sulfide form thereof, said catalyst being produced by a method comprising at least: a) a step of bringing a carbon precursor into contact with a compound based on at least one crystalline aluminium solid, b) a step of thermally treating the solid produced by step a), c) repeating steps a) and b) until the desired deposited carbon content is reached, d) depositing at least one element of group VIB and at least one element of group VIII on the surface of the solid produced by step c), and e) a step of sulfidisation of the solid produced in step d). 1. A process for hydrotreating a hydrocarbon feedstock , which is operated at a temperature of between 180° C. and 450° C. and at a pressure of between 0.5 MPa and 30 MPa , in the presence of a catalyst comprising i) a composite material comprising a compound based on at least one crystalline aluminous solid and carbon , the deposited carbon content being between 1 and 25 weight % of the total mass of the composite material , and ii) at least one element from group VIB and at least one element from group VIII , in their sulfide form ,said catalyst being prepared by a process comprising at least:a) a step of contacting a mixture comprising at least one carbon precursor with a compound based on at least one crystalline aluminous solid, at a temperature of between 50 and 300° C. and at a pressure corresponding at least to the autogenous pressure, the concentration of carbon precursor in said mixture being between 2 and 100 g/l, and the mass ratio of carbon ...

METHOD FOR PRODUCING METAL SUBSTRATE FOR FLUE GAS DENITRATION CATALYST

A metal substrate for flue gas-denitration catalyst that, like SUS304, can be used without corroding is provided by improving the corrosion resistance of SUS430 substrate that is inexpensive and can easily be supplied stably. A method for producing the metal substrate for flue gas-denitration catalyst, wherein the method comprising the steps of: lath-processing a band-shaped steel plate made of ferrite stainless steel into a band-shaped metal lath; (1) degreasing process oil adhering to the metal lath; (2) passing the metal lath through a solution containing phosphoric acid and surfactant to load the solution; (3) draining off the excess solution; and (4) drying and heating the solution-loaded metal lath to react the phosphoric acid with the substrate, in which respective steps are carried out sequentially to form a film of phosphate compound on a surface of the substrate. 1. A method for producing a metal substrate for flue gas-denitration catalyst , wherein the method comprising the steps of:lath-processing a band-shaped steel plate made of ferrite stainless steel into a band-shaped metal lath;(1) degreasing process oil adhering to the metal lath;(2) passing the degreased metal lath through a solution containing phosphoric acid and surfactant to load the solution;(3) draining off the excess solution; and(4) drying and heating the solution-loaded metal lath to react the phosphoric acid with the metal lath,wherein respective steps are carried out sequentially to form a film of phosphate compound on a surface of the metal lath.2. A method for producing a metal substrate for flue gas-denitration catalyst , wherein the method comprising the steps of:lath-processing a band-shaped steel plate made of ferrite stainless steel into a band-shaped metal lath;(1) degreasing process oil adhering to the metal lath;(2) winding the degreased metal lath into a roll;(3) passing the obtained roll through a solution containing phosphoric acid and surfactant to load the solution;(4) ...

Method for Preparing Carbonized Silk Photocatalyst and Use Thereof

Disclosed is a method for preparing a carbonized silk photocatalyst, comprising; soaking a natural silk and an activator in water, taking out the soaked silk, and drying the same; and roasting the dried silk under the protection of an inert atmosphere to prepare a carbonized silk photocatalyst. Also disclosed is a method for photocatalytic desulfurization of a fuel oil, comprising: mixing a fuel oil to be desulfurated, an extraction agent and a carbonized silk photocatalyst, with air being used as an oxidizing agent, to conduct a photocatalytic reaction under light irradiation, and separating an upper oil phase to obtain a desulfurated fuel oil. The catalyst has a simple preparation process, and can effectively reduce dibenzothiophene sulfides, which are difficult to remove, in the fuel oil under UV light radiation. Desulfurization can be achieved at room temperature, and reaction conditions are mild.

PROCESS FOR PREPARING PROPYLENE OXIDE

A continuous process for the preparation of propylene oxide, comprising (i) providing a liquid feed stream comprising propene, hydrogen peroxide, acetonitrile, water, optionally propane, and at least one dissolved potassium salt of a phosphorus oxyacid wherein the molar ratio of potassium relative to phosphorus in the at least one potassium salt of a phosphorus oxyacid is in the range of from 0.6 to 1.4; (ii) passing the liquid feed stream provided in (i) into an epoxidation reactor comprising a catalyst comprising a titanium zeolite of structure type MVVW comprising zinc, and subjecting the liquid feed stream to epoxidation reaction conditions in the epoxidation reactor, obtaining a reaction mixture comprising propylene oxide, acetonitrile, water, the at least one dissolved potassium salt of a phosphorus oxyacid, optionally propene, and optionally propane; (iii) removing an effluent stream from the epoxidation reactor, the effluent stream comprising propylene oxide, acetonitrile, water, at least a portion of the at least one dissolved potassium salt of a phosphorus oxyacid, optionally propene, and optionally propane. 2. The process of claim 1 , wherein the at least one potassium salt of a phosphorus oxyacid has the following formula (I){'br': None, 'sub': nx', '2+n(1-x)', 'n', '3n+1, 'KHPO\u2003\u2003(I)'}wherein n is an integer in a range of from 1 to 10, and wherein x is in a range of from 0.6 to 1.4.3. The process of claim 2 , wherein n is 1.4. The process of claim 2 , wherein x is in a range of from 0.95 to 1.05.5. The process of claim 1 , wherein a weight ratio of water relative to acetonitrile in the liquid feed stream provided in (i) is at most 1:4.6. The process of claim 1 , wherein a molar ratio of potassium comprised in the at least one potassium salt of a phosphorus oxyacid relative to hydrogen peroxide in the liquid feed stream provided in (i) is in a range of from 25×10:1 to 250×10:1.7. The process of claim 1 , wherein the liquid feed stream provided ...

PROCESS FOR PREPARING PROPYLENE OXIDE

A continuous process for the preparation of propylene oxide, comprising (i) providing a liquid feed stream comprising propene, hydrogen peroxide, acetonitrile, water, optionally propane, and at least one dissolved potassium salt; (ii) passing the feed stream provided in (i) into an epoxidation reactor comprising a catalyst comprising a titanium zeolite of structure type MWW, and subjecting the feed stream to epoxidation reaction conditions in the epoxidation reactor, obtaining a reaction mixture comprising propylene oxide, acetonitrile, water, the at least one potassium salt, optionally propene, and optionally pane; (iii) removing an effluent stream from the epoxidation reactor, the effluent stream comprising propylene oxide, acetonitrile, water, at least a portion of the at least one potassium salt, optionally propene, and optionally propane. 1. A continuous process for the preparation of propylene oxide , the process comprising(i) providing a liquid feed stream comprising propene, hydrogen peroxide, acetonitrile, water, optionally propane, and at least one dissolved potassium salt;(ii) passing the feed stream provided in (i) into an epoxidation reactor comprising a catalyst comprising a titanium zeolite of structure MWW, and subjecting the feed stream to epoxidation reaction conditions in the epoxidation reactor, obtaining a reaction mixture comprising propylene oxide, acetonitrile, water, the at least one potassium salt, optionally propene, and optionally propane; and(iii) removing an effluent stream from the epoxidation reactor, the effluent stream comprising propylene oxide, acetonitrile, water, at least a portion of the at least one potassium salt, optionally propene, and optionally propane.2. The process of claim 1 , wherein the at least one potassium salt is selected from the group consisting of at least one inorganic potassium salt claim 1 , at least one organic potassium salt claim 1 , and a combination of at least one inorganic potassium salt and at least ...

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.

METHOD FOR PRODUCING MONOSILANE AND TETRAALKOXYSILANE

The present invention relates to a method for producing monosilane and tetraalkoxysilane comprising subjecting alkoxysilane represented by formula (1) 2. The method for producing monosilane and tetraalkoxysilane as claimed in claim 1 , characterized by use of a catalyst compound represented by formula (II) wherein M is Zr or Ti.3. The method for producing monosilane and tetraalkoxysilane as claimed in claim 1 , characterized by use of a catalyst compound represented by formula (III) wherein M is Zr or Ti.5. The method for producing monosilane and tetraalkoxysilane as claimed in claim 4 , wherein y is 1.3 or 3.7. The method for producing monosilane and tetraalkoxysilane as claimed in claim 6 , using a compound represented by a formula in which Mis K and M is Ti in formula (IIIa):{'br': None, 'sub': 2', '0.5', '2', '2', '5', '0.5, '(KO)(TiO)(PO).'} This is a Divisional application of U.S. application Ser. No. 13/509,118 filed May 10, 2012 which is a 371 of PCT International Application No. PCT/JP2010/070883 filed Nov. 24, 2010, which claims benefit of Japanese Patent Application No. 2009-267094 filed Nov. 25, 2009. The above-noted applications are incorporated herein by reference in their entirety.The present invention relates to a method for producing monosilane and tetraalkoxysilane by disproportionation reaction of alkoxysilane.Monosilane is useful as a volatile silicone material having high purity, and has been widely used for producing solar cells, semiconductors, amorphous photosensitive silicone materials and various ceramic materials.Various methods for producing monosilane have been known to date. A method using reaction between magnesium silicide and acid or ammonium bromide, a method by reducing silicon chloride using LiAlH, a method by reducing silicon tetrafluoride using CaHand a method by disproportionation reaction of alkoxysilane have been known.Trialkoxysilane is generally used as a starting material in the disproportionation reaction of alkoxysilane, ...

CATALYST FOR GLYCERIN DEHYDRATION, PREPARATION METHOD THEREOF, AND PREPARATION METHOD OF ACROLEIN

The present invention relates to a catalyst for glycerin dehydration, a preparation method thereof, and a preparation method of acrolein, and more particularly, to a catalyst for glycerin dehydration which minimizes by-product formation during glycerin dehydration to improve acrolein selectivity and maintains high catalytic activity during reaction. 1. A catalyst for glycerin dehydration , comprising a composite metal oxide represented by the following Chemical Formula 1:{'br': None, 'sub': p', 'q', 'r', 'x, '(Ma)(Mb)WAO\u2003\u2003[Chemical Formula 1]'}wherein A is phosphorus or sulfur,Ma and Mb are the same as or different from each other and are each independently Zr, Ti, Ce, Nb, Cr, Mo, Mn, Zn, B, or Cu, and p and q are a real number of 0 to 3, respectively,when either one of Ma and Mb is B, the other is Zr, Ti, Ce, Nb, Cr, Mo, Mn, Zn, or Cu, and p and q are real numbers of more than 0 and 3 or less,r is a real number of 1 to 3, andx is a real number of 1 to 20.2. The catalyst for glycerin dehydration of claim 1 , wherein a molar ratio of phosphorus or sulfur and tungsten in the composite metal oxide is 10:1 to 1:10.3. The catalyst for glycerin dehydration of claim 1 , wherein a molar ratio of phosphorus or sulfur and tungsten claim 1 , and oxygen in the composite metal oxide claim 1 , is 1:1 to 1:5.4. The catalyst for glycerin dehydration of claim 1 , wherein a molar ratio of Ma or Mb and tungsten in the composite metal oxide is 10:1 to 1:10.5. The catalyst for glycerin dehydration of claim 1 , wherein if Ma and Mb in Chemical Formula 1 are the same as each other claim 1 , Ma and Mb are Zr claim 1 , Ti claim 1 , Ce claim 1 , Nb claim 1 , Cr claim 1 , Mo claim 1 , Mn claim 1 , Zn claim 1 , or Cu.6. The catalyst for glycerin dehydration of claim 1 , wherein the composite metal oxide includes one or more selected from the group consisting of CuWSO claim 1 , CuBWSO claim 1 , CuBWSO claim 1 , NbBWPO claim 1 , NbBWPO claim 1 , NbBWPO claim 1 , NbBWPO claim 1 , NbWPO ...

EXHAUST GAS PURIFICATION CATALYST

The problem to be solved by the present invention is to provide a good NOx selective reduction catalyst. To solve the problem is a NOx selective reduction catalyst containing a composite oxide of Ti, Ce, W, and P or S. 1. A NOx selective reduction catalyst comprising a composite oxide of Ti , Ce , W , and P or S.2. The NOx selective reduction catalyst according to claim 1 , which is of a core/shell type comprising the core part containing zeolite and Cu and the shell part containing the composite oxide. The present invention relates to a NOx selective reduction catalyst. More specifically, the present invention relates to a TiCeW-based NOx selective reduction catalyst capable of selectively reducing nitrogen oxide.When an engine performs combustion in an excess oxygen atmosphere, an exhaust gas containing carbon monoxide, hydrocarbon, nitrogen oxide (NOx), etc., is discharged from the engine. As a catalyst for reducing NOx which is discharged in an oxygen excess atmosphere, by using a reducing agent such as ammonia, a catalyst of a Selective Catalytic Reduction (SCR) type has been known.Under these circumstances, Patent Document 1 describes, for example, a catalyst having supported therein titanium hydroxide, tungstic acid or salts thereof, cerium dioxide, etc., for removing nitrogen oxide by using ammonia as a reducing agent (e.g., claims , and of Patent Document 1).[Patent Document 1] Japanese Unexamined Patent Publication No. 2003-251180However, with respect to the above-described catalytic reduction-type NOx catalyst such as copper-supported zeolite, under high-temperature conditions of, e.g., 500° C., Cu catalyzes an oxidation reaction of NHon the surface of zeolite to produce NOx, and the reducing agent lacks, resulting in that NOx cannot be reduced and the NOx purification rate at high temperatures abruptly decreases. Therefore, a catalytic reduction-type catalyst ensuring a high NOx purification rate at high temperatures has been demanded.As a result of ...

CATALYST FOR GLYCERIN DEHYDRATION, PREPARATION METHOD THEREFOR, AND ACROLEIN PREPARATION METHOD USING CATALYST

The present invention relates to: a catalyst for glycerin dehydration; a preparation method therefor; and an acrolein preparation method using the catalyst. According to one embodiment of the present invention, the catalyst is used in glycerin dehydration so as to exhibit high catalytic activity, a high yield and high acrolein selectivity, and has a characteristic in which carbon is not readily deposited, thereby having a long lifetime compared with that of a conventional catalyst. 1. A catalyst for dehydration of glycerin represented by the following Chemical Formula 1:{'br': None, 'sub': x', 'n', 'y', 'm', 'z, 'ZrA(HPO)\u2003\u2003[Chemical Formula 1]'}in Chemical Formula 1, A is one or more atoms selected from the group consisting of B, W, V, Ca, K, Mg, Sr, Ag, Ni, Zn, Fe, Sn, and Nb; andx, n, m, y, and z represent ratios of atoms or atom groups, wherein x is 0.1 to 6, n is 0.01 to 8, y is 0.1 to 10, m is 1 to 5, and z is 1 to 12.2. The catalyst for dehydration of glycerin according to claim 1 , wherein n is 0.01 to 0.3 claim 1 , m is 4 claim 1 , x is 0.5 to 1 claim 1 , y is 1 to 3 claim 1 , and z is 1 to 5.3. The catalyst for dehydration of glycerin according to claim 1 , wherein the catalyst represented by Chemical Formula 1 is a compound represented by Chemical Formula 2:{'br': None, 'sub': x', 'n1', 'y', '4', 'z, 'sup': '1', 'ZrA(HPO)\u2003\u2003[Chemical Formula 2]'}{'sup': '1', 'in Chemical Formula 2, x is 0.5 to 1, Ais W or Zn, n1 is 0.01 to 0.3, y is 1 to 3, and z is 1 to 5.'}4. The catalyst for dehydration of glycerin according to claim 1 , wherein the catalyst represented by Chemical Formula 1 is a compound represented by Chemical Formula 3:{'br': None, 'sub': x', 'n2', 'n3', 'y', '4', 'z, 'sup': '2', 'ZrAW(HPO)\u2003\u2003[Chemical Formula 3]'}{'sup': '2', 'in Chemical Formula 3, x is 0.5 to 1, Ais B, V, Ca, K, Mg, Ag, Zn, Fe, or Nb, y is 1 to 3, z is 1 to 5, and n2 and n3 are independently a rational number between 0.001 to 0.2 and the sum of n2 and ...

CATALYST FOR GLYCERIN DEHYDRATION, PREPARATION METHOD THEREOF, AND PREPARATION METHOD OF ACROLEIN (As Amended)

The present invention relates to a catalyst for glycerin dehydration, a preparation method thereof, and a preparation method of acrolein, and more particularly, to a catalyst for glycerin dehydration which minimizes by-product formation to improve acrolein selectivity and maintains high catalytic activity during reaction. 1. A catalyst for glycerin dehydration , comprising a heteropolyacid compound including one or more atoms selected from the group consisting of phosphorus (P) and silicon (Si) , and copper (Cu) and tungsten (W).2. The catalyst for glycerin dehydration of claim 1 , wherein a molar ratio of copper and tungsten is 1:5 to 1:10 claim 1 ,000.3. The catalyst for glycerin dehydration of claim 1 , wherein the heteropolyacid compound further includes one or more second metals selected from the group consisting of Zr claim 1 , Ti claim 1 , Ce claim 1 , V claim 1 , Nb claim 1 , Cr claim 1 , Mo claim 1 , Mn claim 1 , Zn claim 1 , B claim 1 , and Cu.4. The catalyst for glycerin dehydration of claim 3 , wherein the second metals are included in an amount of 0.1 to 10 moles with respect to the tungsten claim 3 , respectively.5. The catalyst for glycerin dehydration of claim 1 , wherein the heteropolyacid compound is represented by the following Chemical Formula 1:{'br': None, 'sub': x', 'y', '(12-z', 'z', '40, '(Cu)(H)AW)BO\u2003\u2003[Chemical Formula 1]'}wherein A is phosphorus (P) or silicon (Si),B is selected from the group consisting of Zr, Ti, Ce, V, Nb, Cr, Mo, Mn, Zn, B, and Cu,X is 0.01 to 5,y is 0 to 5, andz is 0 to 12.6. The catalyst for glycerin dehydration of claim 5 , wherein when A is phosphorus (P) claim 5 , y is 3-2x claim 5 , x is 0.01 to 1.5 claim 5 , and y is 0 to 2.98.7. The catalyst for glycerin dehydration of claim 5 , wherein when A is silicon (Si) claim 5 , y is 4-2x claim 5 , x is 0.01 to 2 claim 5 , and y is 0 to 3.98.8. The catalyst for glycerin dehydration of claim 1 , further comprising a support onto which the heteropolyacid compound ...

SOLID OXIDE FUEL CELL

A solid oxide fuel cell includes a cathode including a complex oxide having a perovskite structure expressed by the formula ABO, an anode, and a solid electrolyte layer disposed between the cathode and the anode. The cathode includes phosphorus, chromium and boron, a content amount of the phosphorus in the cathode is at least 10 ppm and no more than 50 ppm, a content amount of the chromium in the cathode is at least 50 ppm and no more than 500 ppm, and a content amount of the boron in the cathode is at least 5 ppm and no more than 50 ppm. 1. A solid oxide fuel cell comprising:{'sub': '3', 'a cathode including a complex oxide having a perovskite structure expressed by the formula ABO,'}an anode, anda solid electrolyte layer disposed between the cathode and the anode, whereinthe cathode includes phosphorus, chromium and boron,a content amount of the phosphorus in the cathode is at least 10 ppm and no more than 50 ppm,a content amount of the chromium in the cathode is at least 50 ppm and no more than 500 ppm, anda content amount of the boron in the cathode is at least 5 ppm and no more than 50 ppm.2. The solid oxide fuel cell according to claim 1 , whereinthe content amount of the phosphorus in the cathode is no more than 30 ppm.3. The solid oxide fuel cell according to claim 1 , whereinthe content amount of the chromium in the cathode is no more than 100 ppm.4. The solid oxide fuel cell according to claim 1 , whereinthe content amount of the boron in the cathode is no more than 10 ppm.5. The solid oxide fuel cell according to claim 2 , whereinthe content amount of the chromium in the cathode is no more than 100 ppm.6. The solid oxide fuel cell according to claim 2 , whereinthe content amount of the boron in the cathode is no more than 10 ppm.7. The solid oxide fuel cell according to claim 3 , whereinthe content amount of the boron in the cathode is no more than 10 ppm. This application is a divisional application of the U.S. application Ser. No. 14/304,434 filed on ...

NOVEL METHOD FOR CATALYTIC DEHYDRATION OF GLYCEROL TO ACROLEIN

A novel method for catalytic dehydration of glycerol to acrolein is provided. A fixed bed reactor is used, which is placed in a microwave unit. The feedstock is introduced into the fixed bed reactor after being preheated and gasified. Continuous glycerol dehydration occurs in the presence of a microwave-absorbing catalyst in the fixed bed reactor to form acrolein. The microwave-absorbing catalyst is composed of an active component loaded on a core-shell structure which consists of microwave absorbent coated by an oxide. The uniformity of microwave heating can reduce the formation of hot spot during the reaction and hence improve the catalyst stability. The process and operation is simple, and the unit can steadily run for a long time. 1. A method for catalytic dehydration of glycerol to acrolein , wherein:a glycerol used as raw material is introduced into a fixed bed reactor after being preheated and gasified in a preheater,the gasified glycerol is then continuously dehydrated to form acrolein in the presence of a microwave-absorbing catalyst in the fixed bed reactor under microwaves generated by a microwave generator.2. The method according to claim 1 , wherein the microwave-absorbing catalyst is denoted as A-MO@MA claim 1 , in which:{'sub': x', 'y', 'x', 'y, 'A represents an active component of the microwave-absorbing catalyst, MOrepresents a coating material, MA represents a microwave absorbent, and the microwave absorbent is coated by the coating material to form a catalyst support of the microwave-absorbing catalyst, denoted as MO@MA.'}3. The method according to claim 1 , wherein the glycerol used is in an aqueous solution with concentration of 10-60 wt % claim 1 , and the glycerol is preheated and gasified at a temperature of 200-300° C. claim 1 , and the glycerol is dehydrated at a temperature of 250-350° C.4. The method according to claim 2 , wherein the active component of the microwave-absorbing catalyst is any one of metal oxide claim 2 , heteropoly acid ...

CATALYST SYSTEM AND PROCESS FOR THE PRODUCTION OF GLYCOLS

The invention provides a catalyst system comprising: a) one or more silver tungstate-containing species; and b) one or more catalytic species suitable for hydrogenation, wherein the weight ratio of said one or more silver tungstate-containing species to the one or more catalytic species suitable for hydrogenation is greater than 2.5:1, on the basis of the total weight of the catalyst system; and a process for the preparation of monoethylene glycol from starting material comprising one or more saccharides, by contacting said starting material with hydrogen in a reactor at a reactor temperature in the range of from 145 to 190 ° C. in the presence of a solvent and said catalyst system. 1. A catalyst system comprising:a) one or more silver tungstate-containing species; andb) one or more catalytic species suitable for hydrogenation, wherein the weight ratio of said one or more silver tungstate-containing species to the one or more catalytic species suitable for hydrogenation is greater than 2.5:1, on the basis of the total weight of the catalyst system.2. The catalyst system according to claim 1 , wherein the one or more catalytic species suitable for hydrogenation are selected from one or more transition metals from Groups 8 claim 1 , 9 or 10 of the Periodic Table claim 1 , or compounds thereof.3. The catalyst system according to claim 1 , wherein the one or more catalytic species suitable for hydrogenation are selected from one or more transition metals selected from the group of cobalt claim 1 , iron claim 1 , platinum claim 1 , palladium claim 1 , ruthenium claim 1 , rhodium claim 1 , nickel claim 1 , iridium claim 1 , and compounds thereof.4. The catalyst system according to claim 1 , wherein the one or more catalytic species suitable for hydrogenation are solid claim 1 , unsupported species.5. The catalyst system according to claim 1 , wherein the one or more catalytic species suitable for hydrogenation are on solid catalyst supports.6. The catalyst system ...

CATALYST SYSTEM AND PROCESS FOR THE PRODUCTION OF GLYCOLS

The invention provides a catalyst system comprising: a) one or more Group 1 metal phosphotungstate-containing species; and b) one or more catalytic species suitable for hydrogenation; and a process for the preparation of monoethylene glycol from starting material comprising one or more saccharides, by contacting said starting material with hydrogen in a reactor in the presence of a solvent and said catalyst system. 1. A catalyst system comprising:a) one or more Group 1 metal phosphotungstate-containing species; andb) one or more catalytic species suitable for hydrogenation.2. The catalyst system according to claim 1 , wherein the one or more Group 1 metal phosphotungstate-containing species are selected from sodium phosphotungstate-containing species and/or caesium phosphotungstate-containing species.3. The catalyst system according to claim 1 , wherein the one or more catalytic species suitable for hydrogenation are selected from one or more transition metals from Groups 8 claim 1 , 9 or 10 of the Periodic Table claim 1 , and compounds thereof.4. The catalyst system according to Claim 1 , wherein the one or more catalytic species suitable for hydrogenation are selected from one or more transition metals selected from the group of cobalt Claim 1 , iron Claim 1 , platinum Claim 1 , palladium Claim 1 , ruthenium Claim 1 , rhodium Claim 1 , nickel Claim 1 , iridium Claim 1 , and compounds thereof.5. The catalyst system according to claim 1 , wherein the one or more catalytic species suitable for hydrogenation are solid claim 1 , unsupported species.6. The catalyst system according to claim 1 , wherein the one or more Group 1 metal phosphotungstate-containing species and/or the one or more catalytic species suitable for hydrogenation are on solid catalyst supports.7. The catalyst system according to claim 6 , wherein the solid catalyst supports are selected from aluminas claim 6 , silicas claim 6 , zirconium oxide claim 6 , magnesium oxide claim 6 , zinc oxide claim 6 , ...

PROCESS FOR PRODUCING ALKENES FROM OXYGENATES BY USING SUPPORTED PARTIALLY NEUTRALISED HETEROPOLYACID CATALYSTS

A process for the vapour phase chemical dehydration of ethanol in a reactor in the presence of a supported hetero-polyacid catalyst, said process comprising a step of contacting the ethanol with the heteropolyacid catalyst, wherein the heteropoly acid catalyst comprises a partially neutralised silicotungstic acid salt, wherein the partially neutralised silicotungstic acid salt has from 30% to 70% of the hydrogen atoms replaced with cations selected from the group consisting of alkali metal cations, alkaline earth metal cations, transition metal cations, ammonium cations, and mixtures thereof; but with the proviso that the alkali metal cation is not lithium; and wherein, after attaining steady-state performance of the catalyst, said process is operated continuously with the same supported heteropolyacid catalyst for at least 150 hours, without any regeneration of the catalyst. 1. A process for the vapour phase chemical dehydration of ethanol in a reactor in the presence of a supported heteropolyacid catalyst , said process comprising a step of contacting the ethanol with the heteropolyacid catalyst ,wherein the heteropolyacid catalyst comprises a partially neutralised silicotungstic acid salt, wherein the partially neutralised silicotungstic acid salt has from 30% to 70% of the hydrogen atoms replaced with cations selected from the group consisting of alkali metal cations, alkaline earth metal cations, transition metal cations, ammonium cations, and mixtures thereof; but with the proviso that the alkali metal cation is not lithium; andwherein, after attaining steady-state performance of the catalyst, said process is operated continuously with the same supported heteropolyacid catalyst for at least 150 hours, without any regeneration of the catalyst.2. A process according to claim 1 , wherein the proportion of hydrogen atoms replaced with other cations in the partially neutralised silicotungstic acid salt is from 40% to 60% claim 1 , preferably from 45% to 55% claim 1 ...

Purification Of Bio Based Acrylic Acid To Crude And Glacial Acrylic Acid

Processes for the purification of bio-based acrylic acid to crude and glacial acrylic acid are provided. The bio-based acrylic acid is produced from hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof. The purification includes some or all of the following processes: extraction, drying, distillation, and melt crystallization. The produced glacial or crude acrylic acid contains hydroxypropionic, hydroxypropionic acid derivatives, or mixtures thereof as an impurity. 1. A composition of crude acrylic acid comprising between about 94 wt % and about 98 wt % acrylic acid , and wherein a portion of the remaining impurities in said composition of crude acrylic acid is hydroxypropionic acid , hydroxypropionic acid derivatives , or mixtures thereof.2. The composition of claim 1 , wherein the hydroxypropionic acid claim 1 , hydroxypropionic acid derivatives claim 1 , or mixtures thereof is lactic acid claim 1 , lactic acid derivatives claim 1 , or mixtures thereof.3. A crude acrylic acid composition produced by the steps comprising:a. Providing an aqueous solution of acrylic acid comprising: 1) acrylic acid; and 2) lactic acid, lactic acid derivatives, or mixtures thereof, and wherein said aqueous solution of acrylic acid is essentially free of maleic anhydride, furfural, and formic acid;b. Extracting said aqueous solution of acrylic acid with a solvent to produce an extract;c. Drying said extract to produce a dried extract;d. Distilling said dried extract to produce a distilled acrylic acid composition; ande. Determining the acrylic acid purity of said distilled acrylic acid composition, and if the purity is less than about 94 wt % acrylic acid, repeating said distilling step on the purified acrylic acid composition until a purity of about 94 wt % acrylic acid is achieved and said crude acrylic acid composition is produced.4. The composition of claim 3 , wherein the aqueous solution of acrylic acid comprises from about 4 wt % to about 80 wt % acrylic ...

Methods for Preparing Diol

Provided is a method for preparing a diol. In the method, a saccharide and hydrogen as raw materials are contacted with a catalyst in water to prepare the diol. The employed catalyst is a composite catalyst comprised of a main catalyst and a cocatalyst, wherein the main catalyst is a water-insoluble acid-resistant alloy; and the cocatalyst is a soluble tungstate and/or soluble tungsten compound. The method uses an acid-resistant, inexpensive and stable alloy needless of a support as a main catalyst, and can guarantee a high yield of the diol in the case where the production cost is relatively low. 1. A method for preparing a diol , characterized in that the method uses a sugar and hydrogen as starting materials , which are brought into contact with a catalyst in water to prepare a diol; the catalyst used is a composite catalyst , consisting of a main catalyst and a cocatalyst ,whereinthe main catalyst is a water-insoluble acid-resistant alloy;the cocatalyst is a soluble tungstic acid salt and/or an insoluble tungsten compound.2. The method for preparing a diol as claimed in claim 1 , characterized in that the diol is ethylene glycol.3. The method for preparing a diol as claimed in claim 2 , characterized in that the reaction system pH is 1-7; more preferably claim 2 , the reaction system pH is 3-6.4. The method for preparing a diol as claimed in or claim 2 , characterized in that the sugar is selected from one or more of five-carbon monosaccharides claim 2 , disaccharides and oligosaccharides claim 2 , six-carbon monosaccharides claim 2 , disaccharides and oligosaccharides claim 2 , soluble five-carbon polysaccharides claim 2 , and soluble six-carbon polysaccharides.5. The method for preparing a diol as claimed in claim 4 , characterized in that the soluble five-carbon polysaccharides and soluble six-carbon polysaccharides are five-carbon polysaccharides and six-carbon polysaccharides which can dissolve under the reaction conditions of the system.6. The method for ...

COMPOSITION AND METHOD FOR CAPTURE AND DEGRADATION OF PFAS

Materials for binding per- and polyfluoroalkyl substances (PFAS) are disclosed. A fluidic device comprising the materials for detection and quantification of PFAS in a sample is disclosed. The fluidic device may be configured for multiplexed analyses. Also disclosed are methods for sorbing and remediating PFAS in a sample. The sample may be groundwater containing, or suspected of containing, one or more PFAS. 1. A method , comprising: combining the sample with a composite sorbent, thereby sorbing the PFAS to the sorbent to form a PFAS-sorbent, the composite sorbent comprising at least two different materials selected from (a) a metal-organic framework (MOF), a covalent organic framework (COF), a covalent organic polymer (COP), zeolites, mesoporous silica, hierarchical porous carbon in combination with (b) at least one of a polymer, a zeolite, a covalent organic framework, mesoporous silica, a hierarchical porous carbon, a photocatalyst, a carbon nanotube, graphite, graphene, graphene oxide, a Prussian blue analog, or a metal oxide; and', 'separating the PFAS-sorbent from the sample, wherein, 'removing a per- or polyfluoroalkyl substance (PFAS) from a sample by'}{'sub': 6', '4', '4, 'claim-text': '(ii) the polymer, if present, is not poly(ethylene-co-vinyl acetate).', '(i) the MOF, if present, does not comprise [ZrO(OH)] and 1,4-benzodicarboxylic acid (UiO-66), and/or'}2. The method of claim 1 , wherein combining the sample with the composite sorbent comprises flowing the sample through a bed of a column claim 1 , the bed comprising the composite sorbent.3. The method of claim 1 , wherein the sample has a contact time with the composite sorbent within a range of from 1 minute to 24 hours.4. The method of claim 1 , further comprising heating the PFAS-sorbent to a temperature Tsufficient to thermally degrade the PFAS.5. The method of claim 4 , wherein the PFAS-sorbent is heated to the temperature Tfor a time period of from 1-24 hours.6. The method of claim 4 , wherein ...

Method for the catalytic conversion of glycerol to propanol

In a method, device, catalyst and a method for producing a catalyst for the catalytic conversion of a substance mixture containing glycerol to propanol in a fixed-bed reactor, substrates of the catalyst have inorganic materials and/or metal oxides. The substrates have a pore diameter at the surface of between 10 and 25 angstroms, preferably between 12 and 20 angstroms, particularly preferably 15 angstroms.

Methods for making supported chromium catalysts with increased polymerization activity

Methods for making a supported chromium catalyst are disclosed, and can comprise contacting a silica-coated alumina containing at least 30 wt. % silica with a chromium-containing compound in a liquid, drying, and calcining in an oxidizing atmosphere at a peak temperature of at least 650 °C to form the supported chromium catalyst. The supported chromium catalyst can contain from 0.01 to 20 wt. % chromium, and typically can have a pore volume from 0.5 to 2 mL/g and a BET surface area from 275 to 550 m 2 /g. The supported chromium catalyst subsequently can be used to polymerize olefins to produce, for example, ethylene-based homopolymers and copolymers having high molecular weights and broad molecular weight distributions.

Methods for making supported chromium catalysts with increased polymerization activity

Methods for making a supported chromium catalyst are disclosed, and can comprise contacting a silica-coated alumina containing at least 30 wt. % silica with a chromium-containing compound in a liquid, drying, and calcining in an oxidizing atmosphere at a peak temperature of at least 650° C. to form the supported chromium catalyst. The supported chromium catalyst can contain from 0.01 to 20 wt. % chromium, and typically can have a pore volume from 0.5 to 2 mL/g and a BET surface area from 275 to 550 m 2 /g. The supported chromium catalyst subsequently can be used to polymerize olefins to produce, for example, ethylene-based homopolymers and copolymers having high molecular weights and broad molecular weight distributions.

Process for producing alkenes from oxygenates by using supported heteropolyacid catalysts

The present invention relates to a supported heteropolyacid catalyst, to a process for producing alkenes from oxygenates in the presence of said catalyst, and to the use of said catalyst in a process for producing alkenes from oxygenates at a higher productivity whilst reducing the formation of alkanes.

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.

Process for producing ethyl acetate

Ethyl acetate is produced in good yield by reacting ethylene with acetic acid in the presence of a catalyst comprising a tungstophosphoric acid of which 10-90% of the total amount of proton is replaced with a member selected from the group consisting of (a) cesium metal cation, (b) a combination of cesium metal cation and at least one cation selected from alkali metal cations other than cesium cation, and (c) a combination of cesium metal cation and at least one cation of iron group metal cations.

Hydrocarbon conversion catalysts

HYDROCARBON CONVERSION CATALYSTS OF IMPROVED ACTIVITY ARE OBTAINED BY ACTIVATING FORMAMINOUS REFRACTORY OXIDES COMBINED WITH AT LEAST ONE THERMALLY DECOMPOSABLE AND/ OR OXIDIZABLE COMPOUND OF A CATALYTICALLY ACTIVE METAL UPON CALCINATION WHILE CONTACTING THE COMPOSITE WITH AN ACCELERATED FLOW OF AN OXIDIZING GAS AT A RATE OF AT LEAST ABOUT 2 S.C.F.M. PER POUND OF SAID COMPOSITE. FURTHER ADVANTAGE IS REALIZED BY HEATING THE COMPOSITE TO THE PRESCRIBED CALCINATION TEMPERATURE AT A CONTROLLED GRADUAL RATE. IT IS ALSO GENERALLY DESIRABLE TO ASSURE THAT THE INLET TEMPERATURE OF THE OXIDIZING GAS PRIOR TO CONTACT WITH THE COMPOSITE IS LESS THAN ABOUT 500*F.

Catalyst having high metal retention capacity and good stability for use in the demetallization of heavy crudes and method of preparation of same

A new active stable catalyst for use in the removal of sulphur, nitrogen, contaminating metals, asphaltenes and Conradson carbon from heavy crudes and residues and, in particular, a method for the preparation of the catalyst and a process for the treatment of heavy crudes and residues with the catalyst. The catalyst comprises a hydrogenation component selected from Group VIB of the Periodic Table, a hydrogenation component selected from Group VIII of the Periodic Table and a phosphorus oxide component as active components all supported on an alumina carrier. The catalyst is made up of a dispersion of the above metals on the surface of the alumina carrier such that, when the catalyst is sulphided under specific conditions, catalytic activities such as hydrodesulphurization (HDS), hydrodenitrogenation (HDN) and hydrodemetallization (HDM) and the conversion of asphaltenes and Conradson carbon are improved.

High activity catalysts

Proceso para producir alquenos de oxigenados utilizando catalizadores de heteropoliacidos soportados.

La presente invención se relaciona a un catalizador de heteropoliácido soportado, a un proceso para producir alquenos de oxigenados en la presencia de dicho catalizador y al uso de dicho catalizador en un proceso para producir alquenos de oxigenados a una alta productividad aunque evitando la formación de alcanos.

methods for producing supported chromium catalysts with increased polymerization activity

MÉTODOS PARA PRODUZIR CATALISADORES DE CROMO SUPORTADOS COM ATIVIDADE DE POLIMERIZAÇÃO AUMENTADA. Métodos para produzir um catalisador de cromo suportado são divulgados e podem compreender colocar uma alumina revestida com sílica contendo pelo menos 30% em peso de sílica em contato com um composto contendo cromo em um líquido, secar e calcinar em uma atmosfera oxidante a uma temperatura de pico de pelo menos 650°C para formar o catalisador de cromo suportado. O catalisador de cromo suportado pode conter de 0,01 a 20% em peso de cromo e, normalmente, pode ter um volume de poro de 0,5 a 2 ml/g e uma área de superfície BET de 275 a 550 m²/g. O catalisador de cromo suportado subsequentemente pode ser usado para polimerizar olefinas para produzir, por exemplo, homopolímeros e copolímeros à base de etileno tendo pesos moleculares elevados e distribuições de peso molecular amplas. METHODS TO PRODUCE CHROME CATALYST SUPPORTED WITH INCREASED POLYMERIZATION ACTIVITY. Methods for producing a supported chromium catalyst are disclosed and may comprise placing a silica coated alumina containing at least 30% by weight silica in contact with a chromium containing compound in a liquid, drying and calcining in an oxidizing atmosphere at a temperature of peak of at least 650°C to form the supported chromium catalyst. The supported chromium catalyst may contain from 0.01 to 20% by weight of chromium and typically may have a pore volume of 0.5 to 2 ml/g and a BET surface area of 275 to 550 m²/g. The supported chromium catalyst subsequently can be used to polymerize olefins to produce, for example, ethylene-based homopolymers and copolymers having high molecular weights and broad molecular weight distributions.

Process for the preparation of a lubricating oil

1429494 Hydrocracking; obtaining lubricating oil SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ BV 4 April 1973 [6 April 1972 19 Dec 1972] 16140/73 Heading C5E A wax, e.g. a slack wax from the dewaxing of a residual oil (straight-run or cracked) is hydrocracked at a temperature of 325‹ to 425‹ C. over a catalyst comprising Ni or Co or both, Mo or W or both, fluorine and sulphur on an alumina carrier to form a liquid product of which at least 25% boils above 400‹ C. This product is topped to a temperature between 350‹ and 470‹ C. and then dewaxed to yield a lubricating oil of dynamic viscosity not more than 24P at -17À8‹ C. and kinematic viscosity not less than 7À0 cS. at 98À9‹ C., e.g. a 10 W/30 multigrade oil. The wax obtained in the dewaxing step may be recycled to the hydrocracking step. The product does not need viscosity-index improvers, but other conventional luboil additives may be blended with it.

一种加氢催化剂组合物和加氢处理的方法

本发明涉及一种加氢催化剂组合物和加氢处理的方法，该加氢催化剂组合物包括加氢催化剂I和加氢催化剂II；以体积计并以所述加氢催化剂组合物为基准，所述加氢催化剂I的含量为5‑95％，所述加氢催化剂II的含量为5‑95％；其中，所述加氢催化剂I的制备方法包括：(1)将加氢活性金属组分和有机络合剂负载到载体上，并进行第一干燥并焙烧，得到催化剂前体；(2)将有机络合剂负载到所述催化剂前体上，并进行第二干燥，得到所述加氢催化剂I。将本发明提供的加氢催化剂组合物应用于加氢处理时，活性好，寿命长。

Method for producing catalyst for hydrotreating hydrocarbon oil

Method for producing hydrotreating catalyst from hydrogel

Process for the preparation of hydrotreating catalysts from hydrogels

Process for producing product of hydrogenolysis of polyhydric alcohol

PROCESS FOR PRODUCING PRODUCT OF HYDROGENOLYSIS OF POLYHYDRIC ALCOH ABSTRACT THE PRESENT INVENTION RELATES TO A PROCESS FOR PRODUCING HYDROGENOLYSIS PRODUCTS OF POLYHYDRIC ALCOHOLS WITH A HIGH SELECTIVITY AS WELL AS HYDROGENOLYSIS CATALYSTS USED IN THE HYDROGENOLYSIS REACTION. THE PRESENT INVENTION PROVIDES 5 A PROCESS FOR PRODUCING A HYDROGENOLYSIS PRODUCT OF A POLYHYDRIC ALCOHOL WHICH INCLUDES THE STEP OF REACTING THE POLYHYDRIC ALCOHOL WITH HYDROGEN IN THE PRESENCE OF A CATALYST CONTAINING (A) A PLATINUM-SUPPORTING HETEROGENEOUS CATALYST COMPONENT AND W AT LEAST ONE CATALYST COMPONENT SELECTED FROM THE GROUP CONSISTING OF TUNGSTEN COMPONENTS AND MOLYBDENUM COMPONENTS, OR IN 10 THE PRESENCE OF A CATALYST CONTAINING A HETEROGENEOUS CATALYST COMPONENT FORMED BY SUPPORTING (A') PLATINUM AND THE ABOVE CATALYST COMPONENT (B), ON A COMMON CARRIER; AS WELL AS CATALYSTS FOR HYDROGENOLYSIS OF POLYHYDRIC ALCOHOLS. 15

Система шаруватих каталізаторів для гідроочистки вуглеводhів та спосіб деhітрофікації вуглеводhів

Система шаруватих каталізаторів для гідроочищення вуглеводнів включає каталізатор першого шару, що містить більше 14 мас. % молібдену і має середній розмір пор 75 – 120 Ǻ, переважно 91 – 104 Ǻ, і каталізатор другого шару, що додатково містить титан. Винахід стосується каталітичних систем і способів гідроочищення вуглеводнів шляхом контактування вуглеводнів з воднем в присутності відповідного каталізатора.

Catalyst and process

Catalyst and method for producing polytetrahydrofurane

The invention relates to a catalyst which contains a catalytically active quantity of at least one oxygen-containing molybdenum and/or wolfram compound on an oxidic support material and which has been calcinated at temperatures of 400 to 900° C. after the precursor compound of the catalytically active compounds have been applied to the support material or to a support material precursor. The transport pores for this catalyst each have a diameter of >25 nm and a volume of at least 50 mm 3 /g. The catalyst contains x μmol (wolfram and/or molybdenum)/m 2 molybdenum and/or wolfram, with 10.1<x<20.9 in relation to the finished catalyst, with the oxidic support material having a BET surface area of 135 to 220 m 2 /g. Catalysts of this type are characterized by an acidity of at least 70 μmol/g at pKs<−3 in the dry state and are therfore very active. The invention also relates to a method for producing a catalyst of this type and to the preferred use thereof.

Stable tungsten-phosphorus modified support for a Fischer-Tropsch catalyst

A process to make a Fischer-Tropsch catalyst with improved hydrothermal stability, comprising: a. contacting a crystalline oxide material with a solution of a tungsten and a phosphorus to make a tungsten-phosphorus modified support; b. calcining the tungsten-phosphorus modified support at a temperature less than or equal to 750° C. to make a calcined tungsten-phosphorus modified support that has the improved hydrothermal stability and that can be used to support a Co-loaded Fischer-Tropsch catalyst. A Co-loaded Fischer-Tropsch catalyst having improved hydrothermal stability and higher C5+ hydrocarbon productivity is also provided. A Fischer-Tropsch synthesis process is provided, comprising contacting a gaseous mixture comprising a carbon monoxide and a hydrogen with the Co-loaded Fischer-Tropsch catalyst having the improved hydrothermal stability and higher C5+ productivity, at a pressure of from 0.1 to 3 MPa and at a reaction temperature of from 180 to 260° C., thereby producing a product comprising C5+ hydrocarbons.

Polymerization of olefines with a catalyst of chromium oxide on aluminum orthophosphate

Process for preparation and use of catalyst support

Verfahren zum Polymerisieren von Olefinen

catalyst system and process for glycol production

a invenção fornece um sistema catalisador que compreende: a) uma ou mais espécies que contêm metatungstato de sódio; e b) uma ou mais espécies cata-líticas adequadas para hidrogenação; e um processo para a preparação de monoeti-lenoglicol a partir de material de partida que compreende um ou mais sacarídeos, colocando-se o dito material de partida em contato com hidrogênio em um reator na presença de um solvente e do dito sistema catalisador. The invention provides a catalyst system comprising: a) one or more species containing sodium metatungstate; and b) one or more catalytic species suitable for hydrogenation; and a process for preparing monoethylene glycol from starting material comprising one or more saccharides by contacting said starting material with hydrogen in a reactor in the presence of a solvent and said catalyst system.

Process for preparing ethene

The present invention provides a process for the preparation of ethene by vapour phase chemical dehydration of a feed comprising ethanol, said process comprising contacting the feed with a supported heteropolyacid catalyst in a reactor, wherein the feed temperature is at least 250 ?C and the pressure inside the reactor is at least 0.80 MPa but less than 1.80 MPa.

catalyst system and process for glycol production

a invenção fornece um sistema catalisador que compreende: a) uma ou mais espécies que contêm fosfotungstato de metal de grupo 1; e b) uma ou mais espécies catalíticas adequadas para hidrogenação; e um processo para a prepara-ção de monoetileno glicol a partir do material de partida que compreende um ou mais sacarídeos, colocando-se o dito material de partida em contato com hidrogênio em um reator na presença de um solvente e do dito sistema catalisador. The invention provides a catalyst system comprising: a) one or more group 1 metal phosphotungstate-containing species; and b) one or more catalytic species suitable for hydrogenation; and a process for the preparation of monoethylene glycol from the starting material comprising one or more saccharides, contacting said starting material with hydrogen in a reactor in the presence of a solvent and said catalyst system.

Process for the preparation of tetrahydrofuran

Die Erfindung betrifft ein Verfahren zur Herstellung von THF (Tetrahydrofuran) durch Umsetzung einer 1,4-Butandiol enthaltenden Reaktionsmischung an einer Heteropolysäure, wobei die Reaktionsmischung, bezogen auf die Heteropolysäure, weniger als 0,2 Gew.-% Eisenionen aufweist. The invention relates to a process for the preparation of THF (tetrahydrofuran) by reacting a 1,4-butanediol-containing reaction mixture over a heteropoly acid, wherein the reaction mixture, based on the heteropolyacid, less than 0.2 wt .-% iron ions.

Lanthanide metal salts of heteropolyanions as catalysts for alcohol conversion

A new catalyst system for the conversion of short-chain aliphatic alcohols to hydrocarbon having the formula [M].sup.m+ [X.sup.p+ Y.sub.a Z.sub.12-a O.sub.40 ].sup.-(8-p) wherein M is selected from at least one element from Group IIIA including lanthanides and actinides, or mixtures thereof, X is at least one element selected from P, Si, As, Ti, Zr, B, Co, Cu or Sn, Y and Z are independently selected from W, Mo, or V, P=is the valence of X usually within 2 to 5, m=8-p O<a≦12.

Improved catalyst and method for producing polytetrahydrofurane

Methods for making supported chromium catalysts with increased polymerization activity

Methods for making a supported chromium catalyst are disclosed, and can comprise contacting a silica-coated alumina containing at least 30 wt. % silica with a chromium-containing compound in a liquid, drying, and calcining in an oxidizing atmosphere at a peak temperature of at least 650 °C to form the supported chromium catalyst. The supported chromium catalyst can contain from 0.01 to 20 wt. % chromium, and typically can have a pore volume from 0.5 to 2 mL/g and a BET surface area from 275 to 550 m2/g. The supported chromium catalyst subsequently can be used to polymerize olefins to produce, for example, ethylene-based homopolymers and copolymers having high molecular weights and broad molecular weight distributions.

Catalyst composition and hydroprocessing of oils using same

A catalyst composition comprising an alumina-aluminum phosphate-silica support bearing a halogen, a Group VI metal and a Group VIII metal in which the support has an average pore radius of from about 10 ANGSTROM to about 300 ANGSTROM , a surface area ranging from about 50 m2/g to about 400 m2/g and a pore volume of about 0.1 to about 1.5 cc/g. The catalyst composition is used for hydroprocessing oils and possesses significant hydrodenitrification activity.

Silica-modified alumina and process for its preparation

A composition of matter comprising alumina as the major component and silica as a minor component is prepared by a process comprising sequential addition of solutions of aluminum salt and alkali metal aluminate, addition of a solution of alkali metal silicate to dispersed alumina hydrogen and heating formed alumina-silica hydrogel under dehydrating conditions. The thus prepared composition of matter, optionally promoted with at least one transition metal compound, can be used as a catalyst for hydrotreating substantially liquid hydrocarbon-containing feed streams which also contain sulfur and metal compounds as impurities.

用于环状碳酸酯合成的催化剂及其制备方法和用途

本发明涉及一种用于合成环状碳酸酯的催化剂，所述催化剂包括一种催化剂活性成分和一个催化剂载体，所述催化剂活性成分包括一种杂多酸，所述催化剂载体的成分包括一种第一过渡金属的金属氧化物，所述金属氧化物选自下列的一种或多种：氧化锆、二氧化钛、氧化锌、氧化硅、氧化铝、五氧化二钒、氧化镁、氧化钙、氧化锡、氧化钡、氧化铈、氧化镧，所述催化剂载体上还包括一种第二过渡金属或第二过渡金属的金属化合物，所述第二过渡金属选自下列的一种或多种：钯、镍、铁、锰、钌、铑、银、锇、铱、铂、金。本发明所提供的催化剂可以促使环氧化合物和二氧化碳反应，合成环状碳酸酯，该反应的反应条件相对温和，催化活性和反应选择性高，反应时间相对较短，此外，本发明所提供的催化剂可以方便地与反应体系分离，可以重复使用，便于放大和工业应用。

一种金属磷酸盐及其制备方法与用于催化酯化反应的应用

本发明公开了一种金属磷酸盐及其制备方法与用于催化酯化反应的应用，所述金属磷酸盐包括单金属磷酸盐或双金属磷酸盐，所述单金属磷酸盐的金属元素是Fe、Cr、Sn、Zr、Ti、Nb中的一种，所述双金属磷酸盐的金属元素是Fe、Cr、Sn、Zr、Ti、Al、Mo、Co、Cu、Nb、Ge、W中的两种，且两种金属元素的摩尔比为1：1。金属磷酸盐用于催化有机羧酸与醇反应生成酯，所述有机羧酸为乙酸、乙酰丙酸、己酸、己二酸、月桂酸、棕榈酸、油酸、苯甲酸、对叔丁基苯甲酸中的一种，所述醇为甲醇、乙醇、丙醇、丁醇中的一种，反应物转化率和产物选择性可达到99%以上，且反应条件温和、反应时间短。

Laminar catalyst system and hydrocarbon denitrofication method

FIELD: preparation of catalysts for petrochemical processes. SUBSTANCE: invention deals with catalysts for hydrodenitration of hydrocarbon systems, for example, vacuum gas oil, applied in hydrocracking process to produce various-type fuels. According to invention, laminar catalyst system contains first catalyst layer based on nickel-molybdenum-phosphorus/alumina or cobalt-molybdenum- phosphorus/alumina and the second catalyst layer constituting nickel- tungsten/silica-alumina-zeolite or nickel-molybdenum/silica-alumina- zeolite catalyst. Preferred features consist in the following: (i) molybdenum content in the first-layer alumina-based catalyst is higher than about 14 wt %; (ii) first-layer alumina-based catalyst has relatively large pore size, e.g. at least some 60 с 9сх60с ПЧ Го РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ ВО ‘” 2 093 263 Сл (51) МПК 65/40//(В 01 4 29/076, 23/883) В 01 4 29/076, С 10 С 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 5010268/04, 09.05.1990 (30) Приоритет: 10.05.1989 Ц$ 349.848 (46) Дата публикации: 20.10.1997 (56) Ссылки: Патент США, 4797155, кл. С 10 С 65/10, 1989. (86) Заявка РСТ: 1$ 9002581 (09.05.90) (71) Заявитель: Чеврон Рисерч Энд Текнолоджи Компани (1$) (72) Изобретатель: Филип Л.Винслоу[Ц$], Ричард Ф.Салливан[0 $] (73) Патентообладатель: Чеврон Рисерч Энд Текнолоджи Компани (Ц$) (54) СИСТЕМА СЛОИСТЫХ КАТАЛИЗАТОРОВ И СПОСОБ ДЕНИТРОФИКАЦИИ УГЛЕВОДОРОДОВ (57) Реферат: Изобретение касается системы слоистых катализаторов — для гидроденитрации углеводородов, например вакуумного газойля, применяемых для гидрокрекинга для получения различного топлива. Система слоистых катализаторов согласно изобретению содержит первый СЛОЙ катализатора на основе никель-молибден-фосфор/окись алюминия или катализатор на основе кобальт-молибден-фосфор/окись алюминия и катализатор второго слоя, представляющий собой катализатор на основе никель-вольфрам/двуокись кремния-окись алюминия-цеолит или катализатор на основе ...

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 ...

Tungsten-based vacancy-keggin-type heteropolyanion for hydrocracking

FIELD: chemistry. SUBSTANCE: invention is intended for chemical industry and can be used in catalysts for hydrocracking, hydroconversion and hydrofining processes. To obtain a heteropoly compound consisting of a nickel salt of vacancy-keggin-type heteropolyanions containing tungsten, x+y/2 equivalents of barium hydroxide are added to heteropolytungstic acids. Ba 2+ cations are then substituted with Ni 2+ cations as a result of ion exchange on cation-exchange resins subjected to exchange with Ni 2+ cations in advance. The obtained heteropoly compound has the formula Ni x+y/2 AW 11-y O 39-5/2y ,zH 2 O, and in another version has the formula Ni x+1 AW 9 O 34 ,zH 2 O, where A is selected from phosphorus, silicon and boron, y=0 or 2, x=3.5, if A denotes phosphorus, x=4, if A denotes silicon, x=4.5, and z is a number from 0 to 36. Nickel atoms are not substituted with tungsten atoms but are located in the counterion position in the structure of said compound. EFFECT: invention provides a high ratio Ni/W and output of more than 80%. 11 cl, 2 dwg, 4 tbl, 4 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 509 729 (13) C2 (51) МПК ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ C01G C01G B01J B01J B01J C10G C10G 41/00 53/00 23/755 23/888 37/30 45/08 49/04 (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2011110473/05, 29.07.2009 (24) Дата начала отсчета срока действия патента: 29.07.2009 C 2 C 2 (56) Список документов, цитированных в отчете о поиске: ISABEL C.M.S. SANTOS et al. Association of Keggin-type anions with cationic meso-substituted porphyrins: synthesis, characterization and oxidative catalytic studies, J. of Molecular Catalysis, A, 2005, v.231, no.1-2, p.p.35-45. RU 2049788 C1, 10.12.1995. US 2547380 A, 03.04.1951. US 2003/0171604 A1, 11.09.2003. US 2003/0208071, 06.11.2003. FR 2749778 A1, 19.12.1997. FR 2764211 A1, 11.12.1998. R U 2 5 0 9 7 2 9 (85) Дата начала рассмотрения заявки PCT на ...

Catalyst for hydrotreating hydrocarbon feeds in a fixed bed reactor

一种异构烷烃与烯烃的烷基化方法

本发明涉及一种异构烷烃与烯烃的烷基化方法，其特征在于使用至少二个并联的反应器，当其中一个或多个反应器中的催化剂需要再生时，在反应器原位通过溶剂与固体酸催化剂接触，冲洗清除覆盖在固体酸催化剂表面上的大分子烃类，恢复催化剂的高选择性。

一种固体酸催化异构烷烃与烯烃的烷基化反应方法

本发明公开了一种固体酸催化异构烷烃与烯烃的烷基化反应方法，是将包括C 4 -C 6 异构烷烃、C 3 -C 6 单键烯烃和作为反应助剂的强电负性元素化合物在内的反应物料与固体酸催化剂接触进行烷基化反应，其特征在于所说的固体酸催化剂在与反应物料接触前，先与含强电负性元素化合物的异构烷烃接触。该方法使烷基化反应目的产物的选择性大大提高，同时也可以提高固体酸催化剂的稳定性。

用于制备乙烯的方法

本发明提供了一种用于通过包含乙醇的进料的气相化学脱水来制备乙烯的方法，所述方法包括使进料与在反应器中的负载杂多酸催化剂接触，其中进料温度是至少250℃并且反应器内部的压力是至少0.80MPa但是小于1.80MPa。

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 ) ...

一种加氢精制催化剂及其制备方法和应用

本发明公开了一种馏分油加氢精制催化剂的制备方法及由该方法制得的催化剂及应用，所述方法包括：(1)用第一浸渍液浸渍载体，然后干燥、焙烧，得到半成品催化剂，所述焙烧条件使得以半成品催化剂的总量为基准，半成品催化剂中炭含量为0.03‑0.5重量％；(2)用第二浸渍液浸渍步骤(1)所得半成品催化剂，然后干燥且不焙烧；其中，所述第一浸渍液为含有加氢活性金属组分的水溶性盐和有机络合剂的酸性水溶液，第二浸渍液为含有有机络合剂的碱性水溶液。与现有技术相比，由本发明所述方法制备的催化剂活性更高，特别适合于馏分油的加氢精制。

탄화수소를 수소화 처리하기 위한 촉매계 및 방법

내용 없음

含磷水合氧化铝组合物和成型体及制备方法和应用以及催化剂及制备方法

本发明公开了一种含磷水合氧化铝组合物和成型体及制备方法和应用以及催化剂及制备方法，该组合物含有水合氧化铝、具有至少两个质子受体位点的化合物和含磷化合物，该组合物的 值为5以下。本发明还公开了以由所述含磷水合氧化铝组合物形成的成型体作为载体的具有加氢催化作用的催化剂及制备方法和加氢处理方法。本发明以水合氧化铝湿凝胶为起始原料制备得到具有较高强度的成型体，省略了用于干燥水合氧化铝湿凝胶的步骤，且在制备成型原料时，无需额外引入水将拟薄水铝石干胶粉调制成可成型的物料，简化了总体工艺流程，降低了总体操作能耗，避免了由于采用拟薄水铝石干胶粉作为原料而引发的粉尘污染，极大的改善了作业环境。

硅掺杂钨酸锌/氧化锌复合材料、制备方法及其应用

硅掺杂钨酸锌/氧化锌复合材料、制备方法及其应用，所述复合材料以磷钨酸和硅钨酸的质量比为1:1～6，硝酸锌与磷钨酸的摩尔比为200～300:1混合制成；硅的掺杂量为0.2～0.8%。所述制备方法为：（1）将磷钨酸和硅钨酸溶于2‑甲基咪唑的甲醇溶液中，混合搅拌；（2）加入硝酸锌甲醇溶液，混合均匀，静置，离心，洗涤，干燥；（3）在氧化气氛中，煅烧，即成。本发明还公开了所述复合材料的应用。本发明复合材料呈碗状颗粒，颗粒平均粒径为120～160nm，碗壁厚10～20nm，在可见光下，90min内的催化降解效果高达92%，重复使用4次后，催化降解效果仍高达86%；本发明方法简单，成本低，适于工业化生产。

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 ...

Methods for Making Supported Chromium Catalysts with Increased Polymerization Activity

Methods for making a supported chromium catalyst are disclosed, and can comprise contacting a silica-coated alumina containing at least 30 wt. % silica with a chromium-containing compound in a liquid, drying, and calcining in an oxidizing atmosphere at a peak temperature of at least 650° C. to form the supported chromium catalyst. The supported chromium catalyst can contain from 0.01 to 20 wt. % chromium, and typically can have a pore volume from 0.5 to 2 mL/g and a BET surface area from 275 to 550 m2/g. The supported chromium catalyst subsequently can be used to polymerize olefins to produce, for example, ethylene-based homopolymers and copolymers having high molecular weights and broad molecular weight distributions.

증가된 중합 활성을 갖는 지지된 크롬 촉매를 제조하는 방법

본원은 지지된 크롬 촉매를 제조하는 방법을 개시하며, 이는 적어도 30 중량%의 실리카를 함유하는 실리카-코팅된 알루미나를 크롬-함유 화합물과 액체 중에서 접촉시키고, 건조시키고, 적어도 650℃의 피크 온도에서 산화 분위기에서 하소하여 상기 지지된 크롬 촉매를 형성하는 단계를 포함할 수 있다. 상기 지지된 크롬 촉매는 0.01 내지 20 중량%의 크롬을 함유할 수 있으며, 전형적으로, 0.5 내지 2 mL/g의 기공 부피 및 275 내지 550 m 2 /g의 BET 표면적을 가질 수 있다. 이어서, 상기 지지된 크롬 촉매는, 예를 들어, 고분자량 및 넓은 분자량 분포를 갖는 에틸렌계 단독 중합체 및 공중합체를 제조하기 위해 올레핀을 중합하는 데 사용될 수 있다.