Process for producing alkylated aromatic compounds and process for producing phenols

According to a process of the invention, a ketone, an aromatic compound and hydrogen as starting materials are reacted together in a single reaction step to produce an alkylaromatic compound in high yield. A process for producing phenols in the invention includes a step of performing the above alkylation process and does not increase the number of steps compared to the conventional cumene process. The process for producing alkylated aromatic compounds includes reacting an aromatic compound such as benzene, a ketone such as acetone and hydrogen in the presence of a solid acid substance, preferably a zeolite, and a silver-containing catalyst.

Process for preparing aromatics from methane

The present invention relates to a process for carrying out endothermic, heterogeneously catalyzed reactions in which the reaction of the starting materials is carried out in the presence of a mixture of inert heat transfer particles and catalyst particles, where the catalyst particles are regenerated in a nonoxidative atmosphere at regular intervals and the heat of reaction required is introduced by separating off the inert heat transfer particles, heating the heat transfer particles in a heating zone and recirculating the heated heat transfer particles to the reaction zone. The process of the invention is particularly suitable for the nonoxidative dehydroaromatization of C 1 -C 4 -aliphatics in the presence of zeolite-comprising catalysts.

Methane aromatization catalyst, method of making and method of using the catalyst

A catalyst for converting methane to aromatic hydrocarbons is described herein. The catalyst comprises an active metal or a compound thereof, and an inorganic oxide support wherein the active metal is added to the support in the form of metal oxalate. The metal oxalate-derived catalyst exhibits superior performance in the conversion of methane-rich feed to aromatics products relative to catalysts prepared from non-oxalate metal precursors. A method of making the catalyst and a method of using the catalyst are also described.

Dehydrogenation Process

In a dehydrogenation process a hydrocarbon stream comprising at least one non-aromatic six-membered ring compound and at least one five-membered ring compound is contacted with a first catalyst comprising at least one metal component and at least one support and a second catalyst. The first catalyst is utilized to convert at least a portion of the at least one non-aromatic six-membered ring compound in the hydrocarbon stream to at least one aromatic compound and the second catalyst is utilized to convert at least a portion of the at least one five-membered ring compound in the hydrocarbon stream to at least one paraffin.

Process for alkylation of toluene to form styrene and ethylbenzene

A process is disclosed for making styrene and/or ethylbenzene by reacting toluene with a C 1 source over a catalyst in at least one radial reactor to form a product stream comprising styrene and/or ethylbenzene.

Production of renewable aromatic compounds

The invention provides a process for producing a variety renewable aromatic compounds such as benzene, toluene, xylenes, and cumene, as well as compounds derived from these including, for example, aniline, benzoic acid, cresol, cyclohexane, cyclohexanone, phenol and bisphenol A, toluene di-isocyanate, isophthalic acid, phthalic anhydride, terephthalic acid and dimethyl terephthalate. The invention also provides for renewable forms of these aromatic compounds.

Palladium Catalysts Supported on Carbon for Hydrogenation of Aromatic Hydrocarbons

Provided is a process for preparing partially or fully hydrogenated hydrocarbons through hydrogenation of aromatic hydrocarbons in the presence of a hydrogenation catalyst. The hydrogenation catalyst comprises palladium deposited on carbon with optional acid wash and calcination treatments and with optional additions of silver and/or alkali metals. 1. A chemical catalyst , comprising an acid-washed carbon base and palladium deposited on said carbon base.2. The chemical catalyst of claim 1 , wherein said carbon base is an activated carbon base.3. The chemical catalyst of claim 1 , wherein said carbon base is calcinated before said palladium is deposited thereon.4. The chemical catalyst of claim 1 , wherein said catalyst comprises from about 0.1 to about 5 weight percentage of palladium.5. The chemical catalyst of claim 1 , further comprising a metal additive deposited on said carbon base with said palladium.6. The chemical catalyst of claim 5 , wherein the molar ratio of said palladium to said metal additive is in a range of from 1:1 to 12:1.7. The chemical catalyst of claim 5 , wherein said metal additive comprises a metal selected from the group consisting of alkali metals and silver.8. A method of making a chemical catalyst claim 5 , comprising the steps of:(i) dissolving a first precursor in deionized water to form a solution;(ii) depositing said solution onto an acid-washed carbon base; and(iii) drying said carbon base in the presence of static air.9. The method of claim 8 , wherein step (ii) is conducted according to the incipient wetness method.10. The method of claim 8 , wherein said carbon base is an activated carbon base.11. The method of claim 8 , further comprising the step of calcining said carbon base prior to the performance of step (ii).12. The method of claim 11 , wherein no calcination treatment is applied to said carbon base following the performance of step (ii).13. The method of claim 11 , wherein said calcining step involves subjecting said ...

Process for Converting Butanol into Propylene

Process for selective the conversion of primary C4 alcohol into propylene comprising: contacting a stream () containing essentially a primary C4 alcohol with at least one catalyst at a temperature ranging from 150° C. to 500° C. and at pressure ranging from 0.01 MPa to 10 MPa conditions effective to transform said primary C4 alcohol into an effluent stream () containing essentially propylene, carbon monoxide and di-hydrogen, said transformation of primary C4 alcohol comprising at least a reaction of decarbonylation and optionally a decarboxylation reaction, said at least one catalyst comprising a support being a non-acidic i.e. having a TPD NH3 of less than 50 preferably less than 40 μmol/g and optionally a non-basic catalyst i.e. having a TPD CO2 of less than 100 preferably less than 50 μmol/g. 115.-. (canceled)16. A process for the conversion of primary C4 alcohol into propylene comprising:{'b': 1', '2', '5, 'contacting a stream () containing a primary C4 alcohol with at least one catalyst at a temperature ranging from 150° C. to 500° C. and at pressure ranging from 0.01 MPa to 10 MPa to transform the primary C4 alcohol into an effluent stream (, ) containing propylene, carbon monoxide and di-hydrogen, the transformation of primary C4 alcohol comprising at least a reaction of decarbonylation and optionally a decarboxylation reaction, the at least one catalyst comprising support which is non-acidic, having a TPD NH3 of less than 50 μmol/g and which is also a non-basic, having a TPD CO2 of less than 100 μmol/g.'}17125. The process according to wherein stream () is contacted with the at least one catalyst to produce an effluent stream ( claim 16 , ) wherein at least 1 wt % of primary C4 alcohol is converted into propylene claim 16 , carbon monoxide and di-hydrogen.181121. The process according to claim 16 , wherein the step of contacting the primary C4 alcohol stream () with the at least one catalyst is performed in a single reaction zone (A) and the at least one ...

Photocatalytic Conversion of Carbon Dioxide and Water Into Substituted or Unsubstituted Hydrocarbon(s)

A method for the production of hydrocarbon(s), such as methane, substituted hydrocarbons, such as methanol, or the production of hydrogen, the method comprising the steps of contacting a first catalyst with water in order to photocatalyse the splitting of at least some of the water into hydrogen and oxygen; and contacting a second catalyst with a gas stream comprising carbon dioxide and at least some of the hydrogen produced from step (a) in order to photocatalyse the reaction between the hydrogen and carbon dioxide to produce hydrocarbon(s), such as methane, and/or substituted hydrocarbons, such as methanol. In an embodiment, the catalyst comprises gold and or ruthenium nanoclusters supported on a substrate. 1. A method for the production of hydrocarbon(s) , such as methane , or substituted hydrocarbons , such as methanol , the method comprising the steps of:contacting a catalyst with water and carbon dioxide in the presence of light in order to photocatalyse:(i) the splitting of at least some of the water into hydrogen and oxygen; and(ii) the reaction between hydrogen and carbon dioxide to produce at least one of a hydrocarbon and/or substituted hydrocarbons;wherein the catalyst comprises at least gold and ruthenium, in the form of at least one nanocluster supported by a substrate.2. The method according to claim 1 , wherein support substrate is selected from the group comprising graphene claim 1 , graphite claim 1 , carbon black claim 1 , nanotubes claim 1 , fullerenes claim 1 , zeolites claim 1 , carbon nitrides claim 1 , metal nitrides and or oxides including zinc oxide or titanium oxide.3. The method according to claim 1 , wherein the gold and ruthenium nanocluster has at least one Au—Ru bond having a distance in the range of from about 2.5 to 3.0 Å.4. The method according to claim 1 , wherein the gold and ruthenium nanocluster comprise an average cluster size less than about 2 nm.5. A method for the production of hydrocarbon(s) claim 1 , such as methane claim ...

SUPPORTED BIMETALLIC CORE-SHELL STRUCTURE CATALYST AND ITS PREPARATION METHOD

The purpose of the invention is to provide a supported bimetallic core-shell structure catalyst and its preparation method. Supporter, metal salt and reducing agent solution are mixed to synthesize the catalyst M@PdM/ZT by using a one-step synthesis method, wherein the active metal particle M@PdM as core-shell structure, M Is the core representing one of the Ag, Pt, Au and Ir. ZT is the supporter, representing one of hydrotalcite (MgAl-LDH), alumina (AlO) and silica (SiO). By changing the temperature and the reaction time to control the kinetic behavior of the reduction of two kinds of metal ions to realize the construction of core-shell structure. Active metal particle composition and shell thickness are regulated by controlling metal ion concentration. The bimetallic core-shell catalyst prepared by this method showed excellent selectivity and stability in acetylene selective hydrogenation and anthraquinone hydrogenation. 1. A preparation method of supported bimetallic core-shell catalyst comprising:{'sub': 3', '6', '5', '7', '2', '2', '2', '6', '2', '5', '7', '2', '3', '4', '2', '2', '3', '2', '5', '7', '2', '2', '3', '2', '2', '3', '2, 'adding M salt and Pd salt to a reducing solution to obtain a mixed salt solution after ultrasonic irradiation for 4-5 min; wherein a total concentration of M and Pd ions is 0.01-20 mmol/L, a molar ratio of M:Pd ions is 0.1 to 10; M is one of Ag, Pt, Au and Ir; M salt is one of AgNO, HPtCl, Pt(CHO), HIrCl.6HO, Ir(CHO)and HAuCl.4HO; Pd salt is one of the PdCl, Pd(NO), Pd(CHO), Pd(CHCOO); the reducing solution is a mixture of reducing agent and deionized water, wherein, a mass ratio of the deionized water is 0-20%; the reducing agent is one of ethylene glycol, isopropanol, N, n-dimethyl acetamide, N, n-dimethyl formamide and glyceraldehyde; stirring and heating the mixed salt solution for 10-30 min under 40-50° C., adding a supporter and continuing to stir for 10-20min; raising temperature to 100-160° C. and keeping the temperature ...

PREPARATION METHOD OF PLATINUM/TIN/METAL/ALUMINA CATALYST FOR DIRECT DEHYDROGENATION OF n-BUTANE AND METHOD FOR PRODUCING C4 OLEFINS USING SAID CATALYST

The provided is a method for preparing a platinum-tin-metal-alumina catalyst by comprising: as an active ingredient, platinum which has a high activity in a direct dehydrogenation reaction of n-butane, tin which can increase the catalyst stability by preventing carbon deposition; additionally metal for reducing the level of catalyst inactivation over the reaction time; and an alumina carrier for supporting said components. Further, provided is a method for producing a high value product, C4 olefins from low cost n-butane by using the catalyst prepared by the method according to the present invention in a direct dehydrogenation reaction.

CATALYST COMPRISING DISPERSED GOLD AND PALLADIUM, AND ITS USE IN SELECTIVE HYDROGENATION

A catalyst comprising gold, palladium, and a porous support, in the form of at least one grain, in which: 1. A catalyst comprising gold , palladium , and a porous support , in the form of at least one grain , in which:the gold content in the catalyst is in the range 0.5% to 3% by weight with respect to the total weight of catalyst;the mean particle size of the gold, estimated by transmission electron microscopy (TEM), is in the range 0.5 nm to 5 nm;the gold is distributed homogeneously in said porous support;at least 80% by weight of the palladium is distributed in an eggshell at the periphery of said porous support;the gold/palladium molar ratio is more than 2.2. The catalyst as claimed in claim 1 , characterized in that the mean particle size of the gold claim 1 , estimated by transmission electron microscopy claim 1 , is in the range 0.5 nm to 3 nm.3. The catalyst as claimed in claim 1 , characterized in that the metallic dispersion D of the gold is in the range 30% to 100%.4. The catalyst as claimed in claim 1 , characterized in that the palladium content is in the range 0.01% to 0.6% by weight with respect to the total weight of catalyst.5. The catalyst as claimed in claim 1 , characterized in that the thickness of said eggshell at the periphery of the porous support is less than 300 μm.6. A process for the preparation of a catalyst as claimed in claim 1 , comprising gold claim 1 , palladium claim 1 , and a porous support claim 1 , in the form of at least one grain claim 1 , said process comprising the following steps:a step termed step 1, in which the palladium is introduced onto the support, comprising the following steps:1a) preparing an aqueous solution of palladium oxide or palladium hydroxide;1b) impregnating said solution onto at least one grain of porous support;1c) maturing the impregnated porous support obtained in step 1b) in order to obtain a catalyst precursor;1d) drying the catalyst precursor obtained in step 1c) at a temperature in the range 50° ...

METHOD OF METHYL CYCLOPENTENE PRODUCTION FROM CYCLOHEXENE OVER ZEOLITE-BASED CATALYST STRUCTURE

Selective conversion from cyclohexene to methylcyclopentene can occur via skeletal isomerization reaction under mild temperature and near atmospheric pressure with the existence of a catalyst structure as described herein. The catalyst structure includes a porous zeolite as the support and one or more loaded metals to further modify its acidity and pore structures. Industrially available cyclohexene feedstock can be effectively converted to a high value-added product methylcyclopentene with over 90 wt % conversion and 95 wt % selectivity, which is highly profitable for potential application in the fine chemical industry. 1. A method for producing methylcyclopentene from cyclohexene via skeletal isomerization , the method comprising:reacting cyclohexene within a reactor in the presence of a gas atmosphere and a catalyst structure, wherein the catalyst structure comprises a porous support structure and one or more metals loaded in the porous support structure, the porous support structure comprises an aluminosilicate material, and the one or more metals loaded in the porous support structure is selected from the group consisting of Na, K, Co, Mo, Ag, Ga and Ce.2. The method of claim 1 , wherein the porous support structure includes Co and/or Mo.3. The method of claim 1 , wherein the gas atmosphere comprises a pure gas or a mixture of two or more gases selected from the group consisting of nitrogen claim 1 , helium claim 1 , methane claim 1 , and argon.4. The method of claim 1 , wherein the aluminosilicate material is selected from the group consisting of HZSM-5 type zeolite claim 1 , L-type zeolite claim 1 , HX type zeolite claim 1 , and HY type zeolite.5. The method of claim 1 , wherein each metal loaded in the porous support structure is present in an amount from 0.1 wt % to 20 wt % by weight of the catalyst support structure.6. The method of claim 5 , wherein the one or more metal components is loaded in the porous support structure as one or more salts selected ...

Catalytic composition and process for the dehydrogenation of butenes or mixtures of butanes and butenes to give 1,3-butadiene

The present invention relates to a dehydrogenation process starting from reagents selected from single butenes, or mixtures thereof, or mixtures of butenes with butanes, to give 1-3 butadiene using catalytic composition of microspheroidal alumina and an active component containing a mixture comprising Gallium and/or Gallium oxides, Tin and/or Tin oxides, a quantity ranging from 1 ppm to 500 ppm with respect to the total weight of the catalytic composition of platinum and/or platinum oxides, and oxides of alkaline and/or alkaline earth metals.

CATALYST REGENERATION

The present disclosure provides an air-soak containing regeneration process reducing its time. The process includes (i) removing surface carbon species from a gallium-based alkane dehydrogenation catalyst in a combustion process in the presence of a fuel gas; (ii) conditioning the gallium-based alkane dehydrogenation catalyst after (i) in air-soak treatment at a temperature of 660° C. to 850° C. with (iii) a flow of oxygen-containing gas having (iv) 0.1 to 100 parts per million by volume (ppmv) of a chlorine source selected from chlorine, a chlorine compound or a combination thereof; and achieving a predetermined alkane conversion percentage for the gallium-based alkane dehydrogenation catalyst undergoing the air-soak containing regeneration process using (i) through (iv) 10% to 50% sooner in air-soak treatment than that required to achieve the same predetermined alkane conversion percentage for the gallium-based alkane dehydrogenation catalyst undergoing the air-soak containing regeneration process using (i) through (iii), but without (iv). 1. A method of reducing a time of an air-soak treatment in a regeneration process , comprising:(i) removing surface carbon species from a gallium-based alkane dehydrogenation catalyst in a combustion process using a fuel gas;(ii) conditioning the gallium-based alkane dehydrogenation catalyst after (i) in the air-soak treatment at a temperature of 660 degree Celsius (° C.) to 850° C. with (iii) a flow of oxygen-containing gas having (iv) 0.1 to 100 parts per million by volume (ppmv) of a chlorine source selected from chlorine, a chlorine compound or a combination thereof; andachieving a predetermined alkane conversion percentage for the gallium-based alkane dehydrogenation catalyst undergoing the air-soak containing regeneration process using (i) through (iv) at least 10% to 50% sooner in air-soak treatment than a time required to achieve the same predetermined alkane conversion percentage for the gallium-based alkane ...

Multimetallic mixed oxides, its preparation and use for the oxidative dehydrogenation of ethane for producing ethylene

A layered multimetallic oxide catalyst having the formula M1 M2 M3 O δ wherein: M1 is selected from the group of Ag, Au, Zn, Sn, Rh, Pd, Pt, Cu, Ni, Fe, Co, an alkaline metal, an alkaline earth metal, a rare earth metal, and mixtures thereof; M2 is selected from the group of Ti, Hf, Zr, Sn, Bi, Sb, V, Nb, Ta and P, and mixtures thereof; M3 is selected from the group of Mo, W and Cr, and mixtures thereof; and where said multilayered metallic oxide exhibits a major X-ray diffraction peak between 5<2θ<15, is prepared by a process of mixing metallic precursors of M 1 , M 2 and M 3 to form a precursor mixture, hydrothermal treatment of the resulting mixture to obtain a homogeneous solid mixture, and thermally treating the solid mixture to activate the solid mixture and obtain said catalyst.

Hydrocarbon Oxidation

A method of direct oxidation of a hydrocarbon to produce an oxygenated reaction product, wherein said method comprises contacting a peroxide and oxygen and the hydrocarbon with a suspension of catalyst particles dispersed in a liquid reaction medium, wherein the catalyst particles are unsupported and comprise at least one transition metal.

METHODS AND APPARATUSES FOR HYDROCARBON PRODUCTION

Methods and apparatuses are provided for producing hydrocarbons. A method for producing hydrocarbons may include two or more reactors having a distributed aromatic rich feed and hydrogen system. Using this configuration, the aromatic rich feed and hydrogen streams are split equally to all reactors wherein each reactor contains a catalyst. The outlet from the last reactor may include a recycle that may be injected into the inlet of the first reactor. 1. A method of producing hydrocarbon compounds comprising:feeding a first aromatic rich feed stream comprising diolefins, a first hydrogen rich stream, and a recycle stream to a first reaction zone comprising a first catalyst to form a first effluent stream comprising mono-olefins; andfeeding a second aromatic rich feed stream comprising diolefins, a second hydrogen rich stream, and first effluent stream to a second reaction zone comprising a second catalyst to form a second effluent comprising mono-olefins wherein a portion of the second effluent stream may be recycled.2. The method of wherein the first reaction zone and the second reaction zone are connected in series.3. The method of wherein the first reaction zone and the second reaction zone may include multiple reactors.4. The method of wherein the first aromatic rich feed stream claim 1 , the first hydrogen stream claim 1 , and the recycle stream are admixed before being fed to the first reaction zone and the second aromatic rich feed stream claim 1 , the second hydrogen stream claim 1 , and the first effluent stream are admixed before being fed to the second reaction zone.5. The method of wherein the recycle stream is reduced by 40-80%.6. The method of wherein the recycle stream is cooled.7. The method of wherein the recycle stream and the feed stream are cooled.8. The method of wherein the first reaction zone and the second reaction zone further comprise independent temperature control.9. The method of wherein the flow rate of the first hydrogen stream and the ...

PROCESS FOR REMOVING CL FROM OXY-DEHYDRO CATALYST

A process for the production of olefins from paraffins is presented. The process converts a paraffin stream through an oxy-dehydrogenation to process stream having olefins. The process includes a continuous catalyst regeneration system, where the catalyst cycles through the reactor and a regenerator. The process includes a treatment step for conditioning the catalyst to remove chloride on the catalyst after regeneration. 1. A process for the regeneration of catalyst for an oxidative dehydrogenation reactor , comprising:passing the catalyst, comprising a noble metal, to a catalyst regenerator to generate a regenerated catalyst stream; andpassing the regenerated catalyst stream to a treatment unit to generate a regenerated stream comprising the catalyst with a chloride (Cl) content less than 1 wt % of the catalyst.2. The process of further comprising passing steam to the treatment unit.3. The process of wherein the treatment unit is operated at a temperature greater than 250° C.4. The process of wherein the Cl content is reduced to less than 0.5 wt % of the catalyst.5. The process of wherein the Cl content is reduced to less than 0.2 wt % of the catalyst.6. The process of further comprising passing the regenerated catalyst stream to an oxidative dehydrogenation reactor claim 1 , wherein the reactor is a moving bed reactor and generates a spent catalyst stream.7. The process of further comprising passing the spent catalyst stream to the catalyst regenerator.8. The process of wherein the catalyst regenerator comprises at least two parts claim 1 , a first combustion section for removing carbon from the catalyst claim 1 , and a second chlorination section for redispersing the noble metal on the catalyst.9. The process of wherein the noble metal is platinum claim 1 , or palladium.10. The process of wherein the catalyst comprises a noble metal claim 1 , and at least one other metal selected from the group consisting of tin (Sn) claim 1 , germanium (Ge) claim 1 , lead (Pb) ...

CATALYST FOR 1,3-BUTADIENE PRODUCTION FROM ETHANOL

The present invention relates to a catalyst for the conversion of ethanol to 1,3-butadiene comprising a support, characterized in that silver (Ag) and copper (Cu) are present on the support in metal form, to a process for producing such a catalyst, to the use of such a catalyst for the conversion of ethanol to 1,3-butadiene, and to a process for the catalytic conversion of ethanol to 1,3-butadiene using such a catalyst. 1. A catalyst for the conversion of ethanol to 1 ,3-butadiene comprising:a support, characterized in that silver (Ag) and copper (Cu) are present on the support in metal form,the support comprising a first metal oxide, the first metal oxide of the support being silica anda second metal oxide, which is different from the first metal oxide, the second metal oxide being magnesium oxide.2. The catalyst according to claim 1 , wherein the silica of the support is silica fume.3. The catalyst according to claim 1 , wherein the magnesium oxide is nano-sized magnesium oxide.4. The catalyst according to claim 1 , wherein the weight ratio between the first metal oxide and the second metal oxide in the support is in the range of 100:1 to 1:100.5. The catalyst according to claim 1 , wherein the weight ratio between silver (Ag) and copper (Cu) on the support is in the range of 10:1 and 1:10.6. The catalyst according to claim 1 , wherein the particle size of the catalyst is between 1 and 100 μm claim 1 , measured by electron microscopy (SEM) according to ASTM standard E986:04.7. The catalyst according to claim 1 , wherein the combined weight (metal loading) of Ag and Cu present on the support is in the range of 1% and 30% claim 1 , based on the total weight of the catalyst claim 1 , measured by X-ray fluorescence (XRF) techniques according to ASTM standard D4326:04.8. The catalyst of claim 1 , wherein the surface area of the catalyst is in the range of 60 to 400 m/g claim 1 , measured by Brunauer-Emmett-Teller method (BET) according to ASTM standard D6556:10.9. The ...

Process for Conversion of Acyclic C5 Compounds to Cyclic C5 Compounds and Catalyst Composition for Use Therein

Disclosed is a process for the conversion of acyclic Cfeedstock to a product comprising cyclic Ccompounds, such as for example, cyclopentadiene, and catalyst compositions for use in such process. The process comprising the steps of contacting said feedstock and, optionally, hydrogen under acyclic Cconversion conditions in the presence of a catalyst composition to form said product. The catalyst composition comprises a Group 10 metal, and, optionally, a Group 11 metal, on a catalyst support with a Group 1 alkali metal silicate and/or a Group 2 alkaline earth metal silicate. 1. A process for conversion of an acyclic Cfeedstock to a product comprising cyclic Ccompounds including cyclopentadiene , said process comprising the steps of contacting said feedstock and , optionally , hydrogen under acyclic Cconversion conditions in the presence of a catalyst composition to form said product , wherein said catalyst composition comprises a Group 10 metal on a catalyst support , with a Group 1 alkali metal silicate and/or a Group 2 alkaline earth metal silicate and , optionally , a Group 11 metal.3. The process of claim 1 , wherein said catalyst composition has Group 10 metal content and claim 1 , optionally claim 1 , a Group 11 metal content in the range from 0.005 wt % to 10 wt % claim 1 , based on the weight of the catalyst composition.4. The process of claim 1 , wherein said Group 10 metal is platinum claim 1 , and said Group 11 metal is copper or silver.5. The process of claim 4 , wherein said source of platinum is selected from the group consisting of platinum nitrate claim 4 , chloroplatinic acid claim 4 , platinous chloride claim 4 , platinum amine compounds claim 4 , platinum acetylacetonate claim 4 , tetraamine platinum hydroxide claim 4 , and mixtures of two or more thereof claim 4 , and/or said Group 11 metal is copper and said source of copper is selected from the group consisting of copper nitrate claim 4 , copper nitrite claim 4 , copper acetate claim 4 , copper ...

CATALYST AND PROCESS FOR THE SELECTIVE CONVERSION OF HYDROCARBONS

A catalyst for a selective conversion of hydrocarbons. The catalyst includes a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof. The catalyst is a support formed as a spherical catalyst particle with a median diameter between 1.6 mm and 2.5 mm and an apparent bulk density between 0.6 and 0.3 g/cc. Also a process of using such a catalyst for a selective hydrocarbon conversion reaction and a process for regenerating such a catalyst by removing coke from same. 1. A catalyst for a selective conversion of hydrocarbons , the catalyst comprising:a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof; anda support forming a catalyst particle, the catalyst particle comprising a plurality of pores, a median diameter between 1.6 mm and 2.5 mm, and an apparent bulk density between 0.6 and 0.3 g/cc,{'sup': −6', '2', '−7', '2, 'wherein the catalyst particle has an effective carbon dioxide diffusivity at 10° C. of at least 1.6×10m/sec, or has an oxygen effective diffusivity at 480° C. of at least 1.5×10m/s, or has both.'}2. The catalyst of wherein the apparent bulk density is between 0.6 and 0.5 g/cc.3. The catalyst of wherein the median diameter is between 1.8 mm and 2.2 mm.4. The catalyst of wherein the median diameter is between 1.8 mm and 2.2 mm.5. The catalyst of wherein the apparent bulk density is between 0.57 to 0.52 g/cc.6. The catalyst of wherein the median diameter is 1.8 mm.7. The ...

Processes for regenerating a catalyst for the selective conversion of hydrocarbons

A catalyst for a selective conversion of hydrocarbons. The catalyst includes a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof. The catalyst is a support formed as a spherical catalyst particle with an average pore diameter between 200 to 350 Angstroms, a porosity of at least 75% and an apparent bulk density between 0.60 and 0.3 g/cc. Also, a process of using such a catalyst for a selective hydrocarbon conversion reaction and a process for regenerating such a catalyst by removing coke from same.

PROCESSES FOR REGENERATING A CATALYST FOR THE SELECTIVE CONVERSION OF HYDROCARBONS

A catalyst for a selective conversion of hydrocarbons. The catalyst includes a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof. The catalyst is a support formed as a spherical catalyst particle with a median diameter between 1.6 mm and 2.5 mm and an apparent bulk density between 0.6 and 0.3 g/cc. Also a process of using such a catalyst for a selective hydrocarbon conversion reaction and a process for regenerating such a catalyst by removing coke from same. 1. A process for reducing a time associated with regenerating a catalyst used for a selective conversion of hydrocarbons , the process comprising:removing coke from a catalyst comprising a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof, and wherein the time associated with regenerating the catalyst is reduced at least 10% compared to a theoretical time for regenerating the catalyst by the catalyst further comprising a support forming a catalyst particle with a median diameter between 1.6 mm and 2.5 mm and an apparent bulk density between 0.6 and 0.3 g/cc.2. The process of wherein the apparent bulk density is between 0.6 and 0.5 g/cc.3. The process of wherein the median diameter is between 1.8 mm and 2.2 mm.4. The process of wherein the median diameter is between 1.8 mm and 2.2 mm.5. The process of wherein the apparent bulk density is between 0.57 to 0.52 g/cc.6. The process of wherein the median diameter is 1.8 mm.7. The process ...

SELECTIVE HYDROGENATION METHODS

The present disclosure relates to methods for selectively hydrogenating acetylene, to methods for starting up a selective hydrogenation reactor, and to hydrogenation catalysts useful in such methods. In one aspect, the disclosure provides a variety of methods for starting up reactors for use in methods for selectively hydrogenating acetylene using a catalyst composition comprises a porous support, palladium, and one or more ionic liquids. 1. A method of starting up a selective hydrogenation reactor , the reactor housing one or more catalyst beds each containing a catalyst suitable for selectively hydrogenating acetylene in a process gas comprising at least 10 mol. % ethylene , at least 1 ppm acetylene , and at least 5 mol. % hydrogen , the method comprisingproviding each catalyst bed at no more than a first temperature, the catalyst of the catalyst bed being in contact with a first gas, the first gas being non-reactive in the presence of the catalyst at the first temperature;in the presence of the first gas, heating each catalyst bed to at least a second temperature, the second temperature being at least 20 degrees greater than the first temperature, the first gas being non-reactive in the presence of the catalyst at the second temperature; and thenchanging the composition of the gas in contact with the catalyst from the first gas to a flow of the process gas while the catalyst bed is at least at the second temperature; andallowing the process gas to flow through the catalyst bed until a concentration of acetylene at an outlet of the reactor is less than 1 ppm.2. The method of claim 1 , wherein the catalyst of each catalyst bed has not been contacted in the reactor with carbon monoxide in an amount in excess of 100 ppm claim 1 , and wherein the method includes refraining from adding carbon monoxide to the process gas.3. A method of starting up a selective hydrogenation reactor claim 1 , the reactor housing one or more catalyst beds each containing a catalyst ...

SELECTIVE HYDROGENATION METHODS

The present disclosure relates to methods for selectively hydrogenating acetylene, to methods for starting up a selective hydrogenation reactor, and to hydrogenation catalysts useful in such methods. In one aspect, the disclosure provides a method for selectively hydrogenating acetylene, the method comprising contacting a catalyst composition with a process gas. The catalyst composition comprises a porous support, palladium, and one or more ionic liquids. The process gas includes ethylene, present in the process gas in an amount of at least 20 mol. %; acetylene, present in the process gas in an amount of at least 1 ppm; and 0 to 190 ppm or at least 600 ppm carbon monoxide. At least 90% of the acetylene present in the process gas is hydrogenated, and the selective hydrogenation is conducted without thermal runaway. 2. A method according to claim 1 , wherein carbon monoxide is present in the process gas in an amount up to 150 ppm.3. A method according to claim 1 , wherein carbon monoxide is present in the process gas in an amount up to 85 ppm.5. A method according to claim 4 , wherein carbon monoxide is present in the process gas in an amount within the range of 1000 ppm to 20 claim 4 ,000 ppm.6. A method according to claim 1 , wherein the process gas is contacted with the catalyst at a gas hourly space velocity (GHSV) within the range of 2 claim 1 ,000 hto 40 claim 1 ,000 h.7. A method according to claim 1 , wherein the process gas is contacted with the catalyst at a GHSV within the range of 7 claim 1 ,100 hto 40 claim 1 ,000 h.8. A method according to claim 1 , wherein the selective hydrogenation is conducted at a temperature within the range of 20° C. to 140° C.9. A method according to claim 1 , wherein at least 95% of the acetylene present in the process gas is hydrogenated.10. A method according to claim 1 , wherein the amount of ethane in the product of the selective hydrogenation is no more than 0.5 mol. % greater than the amount of ethane in the process gas.11 ...

Selective hydrogenation methods and catalysts

The present disclosure relates to methods for selectively hydrogenating acetylene, to methods for starting up a selective hydrogenation reactor, and to hydrogenation catalysts useful in such methods. In one aspect, the disclosure provides a method for selectively hydrogenating acetylene, the method comprising contacting a catalyst composition with a process gas. The catalyst composition comprises a porous support, palladium, and one or more ionic liquids. The process gas includes ethylene, present in the process gas in an amount of at least 20 mol. %; and acetylene, present in the process gas in an amount of at least 1 ppm. At least 90% of the acetylene present in the process gas is hydrogenated, and the selective hydrogenation is conducted without thermal runaway. Notably, the process gas is contacted with the catalyst at a gas hourly space velocity (GHSV) based on total catalyst volume in one bed or multiple beds of at least 7,100 h−1.

DEHYDROGENATION CATALYSTS AND METHODS FOR PREPARING AND USING THEM

The present disclosure relates to dehydrogenation catalysts based on one or more certain group 13 and group 14 elements that further include additional metal components, to methods for making such catalysts, and to methods for dehydrogenating hydrocarbons using such catalysts. One aspect of the disclosure provides a calcined dehydrogenation catalyst that includes a primary species P1 selected from the group consisting of Ga, In, TI, Ge, Sn and Pb and combinations thereof; a primary species P2 selected from the lanthanides; a promoter M1 selected from the group consisting of Ni, Pd and Pt; a promoter M2 selected from the group consisting of Li, Na, K, Rb, Cs, Be, Mg, Ca, Sr and Ba, on a silica-alumina support. 1. A calcined dehydrogenation catalyst comprisinga primary species P1 selected from the group consisting of Ga, In, TI, Ge, Sn, and Pb and combinations thereof, present in the composition in an amount within the range of about 0.05 wt. % to about 20 wt. %, calculated as elemental metal on a calcined basis;a primary species P2 selected from the lanthanides, present in the composition in an amount within the range of about 0.05 wt. % to about 10 wt. %, calculated as elemental metal on a calcined basis;a promoter M1 selected from the group consisting of Ni, Pd, and Pt, present in the composition in an amount within the range of about 10 ppm to about 500 ppm, calculated as elemental metal on a calcined basis;a promoter M2 selected from the group consisting of Li, Na, K, Rb, Cs, Be, Mg, Ca, Sr, and Ba, present in the composition in an amount within the range of about 0.05 wt. % to about 3 wt. %, calculated as elemental metal on a calcined basis; anda silica-alumina support S1, present in the composition in an amount within the range of about 60 wt. % to about 99 wt. %, calculated as oxide on a calcined basis.2. The catalyst composition of claim 1 , wherein P1 is selected from Ga claim 1 , Ge claim 1 , In claim 1 , Sn claim 1 , and TI and combinations thereof.3. The ...

CATALYTIC CONVERSION OF ETHANOL TO 1-/2-BUTENES

Simple and economical conversion of aqueous ethanol feed streams into butenes by a single step method using transition metal oxides on a silica supports under preselected processing conditions. By directly producing a C4-rich olefin mixture from an ethanol containing stream various advantages are presented including, but not limited to, significant cost reduction in capital expenses and operational expenses. 120-. (canceled)21. A process for producing butene from a feed stream containing ethanol in a single step , the process comprising the step of:passing a feed stream containing ethanol in a gas phase over a 0.5 wt. % Au_4 wt. % Ag/4 wt. % ZrO2/SBA-16.catalyst having a transition metal oxide with a transition metal dispersion of at least 30% on a silica support in the presence of a hydrogen containing carrier gas, at a preselected temperature and preselected pressure to directly form butenes from the ethanol with selectivity equal or greater than 13%.22. A process for producing butene from a feed stream containing ethanol in a single step , the process comprising the step of: passing a feed stream containing ethanol in a gas phase over a catalyst having a transition metal oxide with a transition metal dispersion of at least 30% on a silica support in the presence of a hydrogen containing carrier gas , at a preselected temperature and preselected pressure to directly form butenes from the ethanol with selectivity equal or greater than 13% , wherein the catalyst is a 0.5 wt. % Re 4 wt. % Ag/4 wt ,% Zr02/Si02-SBA-16 catalyst.23. A process for producing butene from a feed stream containing ethanol in a single step , the process comprising the step of: passing a feed stream containing ethanol in a gas phase over a catalyst having a transition metal oxide with a transition metal dispersion of at least 30% on a silica support in the presence of a hydrogen containing carrier gas , at a preselected temperature and a pressure of 70 atm to directly form butenes from the ...

SULFUR TERMINATED ORGANOSILICA MATERIALS AND USES THEREOF

Provided herein are compositions and methods for use of an organosilica material comprising a copolymer of at least one monomer of Formula [RRSiCH](I), wherein, Rrepresents a C-Calkoxy group; and Ris a C-Calkoxy group or a C-Calkyl group; and at least one other monomer of Formula [(ZO)ZSi—Z—SZ] (II), wherein, Zrepresents a hydrolysable functional group; Zrepresents a C-Calkyl or aryl group; Zrepresents a C-Ccyclic or linear hydrocarbon; Zis either H or OH; and x represents any one of integers 1, 2, and 3. The composition may be used as a support material to covalently attach transition metal cations, as a sorbent for olefin/paraffin separations, as a catalyst support for hydrogenation reactions, as a precursor for highly dispersed metal nanoparticles, or as a polar sorbent for crude feeds. 1. An organosilica material comprising a copolymer of{'sup': 1', '2, 'sub': 2', '3, 'claim-text': [{'sup': '1', 'sub': 1', '4, 'Rrepresents a C-Calkoxy group; and'}, {'sup': '2', 'sub': 1', '4', '1', '4, 'Ris a C-Calkoxy group or a C-Calkyl group; and'}], 'at least one monomer of Formula [RRSiCH](I), wherein{'sup': 1', '2', '3', '4, 'sub': x', '3-x, 'claim-text': [{'sup': '1', 'Zrepresents a hydrolysable functional group;'}, {'sup': '2', 'sub': 1', '10, 'Zrepresents a C-Calkyl or aryl group;'}, {'sup': '3', 'sub': 2', '11, 'Zrepresents a C-Ccyclic or linear hydrocarbon;'}, {'sup': '4', 'sub': '3', 'Zis either H or OH; and'}, 'x represents any one of integers 1, 2, and 3., 'at least one other monomer of Formula [(ZO)ZSi—Z—SZ] (II), wherein2. The organosilica material of claim 1 , wherein Zhas incorporated within the C-Ccyclic or linear hydrocarbon (a) an amine claim 1 , (b) an ether claim 1 , (c) a heteroatom claim 1 , (d) a combination of any of (a) claim 1 , (b) claim 1 , and (c) claim 1 , or none of (a) claim 1 , (b) claim 1 , and (c) claim 1 , provided that Si and S remain bonded to a carbon atom.3. The organosilica material of claim 1 , further comprising a catalyst metal.4. ...

SILICALITE-1 MOLECULAR SIEVE-BASED CATALYST AND PREPARATION METHOD FOR 1,2-PENTANEDIOL USING SAID CATALYST

An organic-base functionalized silicalite-1 molecular sieve-encapsulated metal nanoparticles catalyst and a preparation method therefor, as well as a method for preparing 1,2-pentanediol from biomass-derived furfuryl alcohol by hydrogenolysis using said catalyst. When the catalyst is used in a reaction preparing 1,2-pentanediol from furfuryl alcohol by hydrogenolysis, the catalyst has high hydrogenolysis activity under relatively mild reaction conditions, significantly increasing the conversion rate of furfuryl alcohol and 1,2-pentanediol selectivity in the reaction, while also not generating obvious byproducts furfuryl alcohol polymers; the catalyst has good stability and long life, and may be recovered for reuse after the reaction is complete by means of a simple filtration, greatly reducing reaction costs and separation difficulty. 1. A catalyst for preparing 1 ,2-pentanediol by hydrogenolysis of furfuryl alcohol , wherein the catalyst comprises a carrier and an active component , the carrier is a silicalite-1 molecular sieve surface-modified with an organic-base silane coupling agent , the active component is metal nanoparticles encapsulated in the pores of the silicalite-1 molecular sieve.3. The catalyst according to claim 1 , wherein the metal nanoparticle is one or more of Ni claim 1 , Co claim 1 , Cu claim 1 , Ru claim 1 , Rh claim 1 , Pd claim 1 , Ir claim 1 , Pt and Au claim 1 , preferably Pt and/or Au.4. The catalyst according to claim 1 , wherein the loading amount of the metal nanoparticle is 0.01-5 wt % claim 1 , based on the mass of the silicalite-1 molecular sieve without surface-modification in the catalyst.5. The catalyst according to claim 4 , wherein the amount of the organic-base silane coupling agent is 0.01-5 mmol/g claim 4 , based on the mass of the silicalite-1 molecular sieve without surface-modification in the catalyst.6. A method for preparing the catalyst according to claim 1 , wherein the method comprises the steps of:a) reducing an ...

METHOD FOR REMOVING DIENES FROM A MATERIAL STREAM CONTAINING C3 TO C5 HYDROCARBONS BY SELECTIVE HYDROGENATION

The invention relates to a process for removing dienes from a material stream comprising Cto Chydrocarbons by selective hydrogenation at a specified reaction pressure and a specified reaction temperature in the presence of a hydrogenation catalyst, wherein the reaction pressure and the reaction temperature at the reactor inlet are regulated such that the reaction pressure at the reactor inlet does not deviate by more than 0.01 bar from the specified reaction pressure and the reaction temperature at the reactor inlet does not deviate by more than 0.1° C. from the specified reaction temperature and the proportion of hydrogen supplied to the selective hydrogenation is in the range from 2 to 20 moles per mole of diene present in the material stream comprising Cto Chydrocarbons. 113.-. (canceled)14. A process for removing dienes from a material stream comprising Cto Chydrocarbons by selective hydrogenation at a specified reaction pressure and a specified reaction temperature in the presence of a hydrogenation catalyst , wherein the reaction pressure and the reaction temperature at the reactor inlet are regulated such that the reaction pressure at the reactor inlet does not deviate by more than 0.01 bar from the specified reaction pressure and the reaction temperature at the reactor inlet does not deviate by more than 0.1° C. from the specified reaction temperature and the proportion of hydrogen supplied to the selective hydrogenation is in the range from 2 to 20 moles per mole of diene present in the material stream comprising Cto Chydrocarbons.15. A process for removing dienes from a material stream comprising Cto Chydrocarbons by selective hydrogenation , comprising the following steps:{'sub': 3', '5', '3', '5', '3', '5', '3', '5, '(a) vaporizing part of a material stream comprising liquid Cto Chydrocarbons, mixing a gaseous material stream comprising Cto Chydrocarbons and a liquid one, or condensing part of a material stream comprising gaseous Cto Chydrocarbons, with ...

A METHOD FOR PRODUCTION OF METHYL METHACRYLATE BY OXIDATIVE ESTERIFICATION USING A HETEROGENEOUS CATALYST

A method for preparing methyl methacrylate from methacrolein and methanol. The method comprises contacting in a reactor a mixture comprising methacrolein, methanol and oxygen with a heterogeneous catalyst comprising a support and a noble metal, wherein said catalyst has an average diameter of at least 200 microns, wherein oxygen concentration at a reactor outlet is from 0.5 to 7.5 mol % and wherein the reactor comprises a partition with the catalyst bed on a first side of the partition and with flow through the catalyst bed in a first direction and flow on a second side of the partition in an opposite direction. 1. A method for preparing methyl methacrylate from methacrolein and methanol; said method comprising contacting in a reactor a mixture comprising methacrolein , methanol and oxygen with a heterogeneous catalyst comprising a support and a noble metal , wherein said catalyst has an average diameter of at least 200 microns , wherein oxygen concentration at a reactor outlet is from 0.5 to 7.5 mol % and wherein the reactor comprises a partition with the catalyst bed on a first side of the partition and with flow through the catalyst bed in a first direction and flow on a second side of the partition in an opposite direction.2. The method of in which the catalyst bed is in the shape of a cylindrical shell located between the partition and the reactor walls.3. The method of in which the catalyst has an average diameter from 400 microns to 10 mm.4. The method of in which the catalyst bed is at a temperature from 40 to 120° C.5. The method of in which the reactor is a continuous stirred tank reactor and height of the partition is from 30 to 90% of height of the reactor.6. The method of in which the continuous stirred tank reactor is configured with liquid flow downward inside the partition and upward through the catalyst bed.7. The method of in which at least 90 wt % of the noble metal is in the outer 70% of catalyst volume.8. The method of in which the noble metal ...

BINDER-FREE HIGH STRENGTH, LOW STEAM-TO-OIL RATIO ETHYLBENZENE DEHYDROGENATION CATALYST

The invention discloses a binder-free high strength and low steam-to-oil ratio ethylbenzene dehydrogenation catalyst, which is characterized by comprising the following components in percentage by weight: (a) 60-85% FeO; (b) 3-25% KO; (c) 0.1-5% MoO; (d) 3-20% CeO; (e) 0.1-5% CaO; (f) 0.1-5% NaO; (g) 0.1-5% MnO, wherein the weight ratio of sodium oxide to manganese dioxide is 0.1-10, and no binder is added during the preparation of the catalyst. The low steam-to-oil ratio ethylbenzene dehydrogenation catalyst provided by the present invention contains no binder and maintains high strength, and has high activity and stability at low steam-to-oil ratio. 1. A binder-free high strength and low steam-to-oil ratio ethylbenzene dehydrogenation catalyst , comprising the following components by weight percentage:{'sub': 2', '3, '(a) 60-85% FeO;'}{'sub': '2', '(b) 3-25% KO;'}{'sub': '3', '(c) 0.1-5% MoO;'}{'sub': '2', '(d) 3-20% CeO;'}(e) 0.1-5% CaO;{'sub': '2', '(f) 0.1-5% NaO;'}{'sub': 2', '2', '2, '(g) 0.1-5% MnO, wherein the weight ratio of NaO and MnOis 0.1-10; and no binder is added during the preparation of the catalyst.'}2. The binder-free high strength claim 1 , low steam-to-oil ratio ethylbenzene dehydrogenation catalyst according to claim 1 , wherein the weight ratio of NaO and MnOis 0.2-8.3. The binder-free high strength and low steam-to-oil ratio ethylbenzene dehydrogenation catalyst according to claim 2 , wherein the weight ratio of NaO and MnOis 0.5-5.4. The binder-free high strength and low steam-to-oil ratio ethylbenzene dehydrogenation catalyst according to claim 1 , further comprising 0.05 to 2% CuO.5. The binder-free high strength and low steam-to-oil ratio ethylbenzene dehydrogenation catalyst according to claim 1 , further comprising 0.05 to 2% ZnO.6. The binder-free high strength and low steam-to-oil ratio ethylbenzene dehydrogenation catalyst according to claim 1 , further comprising 0.05 to 2% MgO.7. The binder-free high strength and low steam-to-oil ...

SELECTIVE HYDROGENATION METHOD

The present subject matter relates generally to methods for selectively saturating the unsaturated C-C. More specifically, the present subject matter relates to methods for saturating butadiene and butenes from a hydrocarbon stream before it is combined with a fresh feed and enters a reaction zone. Removing the unsaturates from the hydrocarbon stream before the hydrocarbon stream enters the reaction zone prevents the reactor internals from coking. 1. A method for saturating hydrocarbons comprising:passing a hydrocarbon stream comprising butadiene to a guard bed wherein the hydrocarbon stream is contacted with an adsorbent to form a treated hydrocarbon stream; andpassing the treated hydrocarbon stream and a hydrogen stream to a reaction zone containing a hydrogenation catalyst to form a reaction zone effluent stream.2. The method of claim 1 , wherein the hydrocarbon stream comprises light paraffins claim 1 , olefins claim 1 , diolefins mainly butadiene claim 1 , and aromatics claim 1 , water claim 1 , hydrogen sulfide claim 1 , and other sulfur containing compounds.3. The method of claim 1 , wherein the treated hydrocarbon stream comprise C-Cparaffin and olefins claim 1 , diolefins mainly butadiene claim 1 , and aromatics.4. The method of claim 1 , wherein the guard beds contains molecular sieves to remove HO.5. The method of claim 1 , wherein the guard beds contains molecular sieves to remove HO and HS.6. The method of claim 1 , wherein the guard beds contain molecular sieves and metal or metal oxides that are capable of going through reduction-oxidation cycle to remove HS and other sulfur containing compounds.7. The method of claim 1 , wherein the reaction zone does not saturate more than 20% of aromatics in the treated hydrocarbon stream.8. The method of claim 1 , wherein the reaction zone comprises multiple reactors in series having inter-stage quenching.9. The method of claim 8 , wherein the inter-stage quenching includes dividing Hand injecting it into ...

SINGLE STEP CONVERSION OF ETHANOL TO BUTADIENE

A process for producing 1,3-butadiene (BD) from ethanol in a single step by s7 passing a mixture containing ethanol in a gas phase over a multifunctional catalyst having a transition metal dispersion of at least 30% on a silica metal oxide support. In some examples the multifunctional catalyst comprises a silica metal oxide having a surface area of at least 200 m̂2/g. The multifunctional catalyst can include a transition metal oxide, a silica metal oxide made from a high purity silica gel, mesoporous silica and fumed silica, such as high purity SBA16, SBA15, or Davisil grade 646. 1. A process for producing 1 ,3-butadiene (BD) from ethanol in a single step , comprising the step of passing a feed containing ethanol in a gas phase over a multi-functional catalyst having a transition metal dispersion of at least 30% on a metal oxide support.2. The process of wherein the multifunctional catalyst comprises a silica metal oxide having a surface area of at least 200 m̂2/g.3. The process of wherein the multifunctional catalyst further comprises a Group 11 metal.4. The process of wherein the Group 11 metal is selected from the group consisting of copper (Cu) claim 3 , silver (Ag) claim 3 , and gold (Au).5. The process of wherein the silica metal oxide support comprises a silica metal oxide selected from the group consisting of a high purity silica gel claim 2 , mesoporous silica and fumed silica.6. The process of wherein the silica metal oxide is a high purity SBA16.7. The process of wherein the silica metal oxide is high purity SBA15.8. The process of wherein the silica metal oxide is Davisil grade 646.9. The process of wherein hydrogen is added to the mixture.10. The process of wherein the feed is 100% ethanol.11. The process of wherein the feed is a mixture containing at least 30 percent ethanol and includes water.12. The process of wherein the step of passing the mixture containing ethanol in a gas phase over a catalyst comprising a silica metal oxide is performed at a ...

PROCESS FOR HYDROGENATION OF OLEFINIC OR ACETYLENIC BONDS

The present invention relates to a process for hydrogenation of olefinic or acetylenic bonds. Further, the present invention relates to a process for selective hydrogenation of olefinic or acetylenic bonds and/including triglycerides using modified metal supported on solid acidic metal oxide catalyst and the process for the preparation thereof. The present invention provides a process for hydrogenation of olefinic or acetylenic bonds using metal supported on solid acid metal oxide based catalyst, at moderate conditions. The present invention also relates to the preparation of metal supported on solid acid metal oxide based catalyst for hydrogenation reactions under mild conditions. 1. A process for hydrogenation of olefinic or acetylenic bonds , said process comprising:a. activating a catalyst in a flow of hydrogen gas in a solvent 10 times volume of the substrate at room temperature ranging between 20-30° C.,b. reacting the catalyst of step (a) with reactant in the range of 1-10 wt % with respect of substrate by stirring for 0.5-15 hours at atmospheric pressure and room temperature (20-30° C.),c. obtaining the desired product from step (b).2. The process according to claim 1 , wherein the catalyst used in step (a) is solid acidic support comprising a metal oxide claim 1 , mixed metal oxides or modified metal oxides.3. The process according to claim 2 , wherein metals selected from group II A claim 2 , IIIA claim 2 , IVA claim 2 , IB claim 2 , IVB claim 2 , VIB claim 2 , and VIIIB.4. The process according to claim 2 , wherein at least one elemental metal dispersed on said support wherein the elemental metal is selected from group VIB claim 2 , IB or VIIIB metals in an amount up to 0.1-1.0 weight percent based upon the total weight of metal and support.5. The process according to claim 1 , wherein yield and selectivity of desired product is up to 100%.6. The process according to claim 1 , wherein the solvent is selected from toluene claim 1 , methanol claim 1 , ...

POLYMER-SUPPORTED TRANSITION CATALYST

A long life catalyst is provided that is conveniently and inexpensively capable of being produced and that is highly active and has inhibited metal leakage. According to aspects of the present invention, a catalyst is provided that includes: a polymer including a plurality of first structural units and a plurality of second structural units; and metal acting as a catalytic center, wherein at least part of the metal is covered with the polymer, each of the plurality of first structural units has a first atom constituting a main chain of the polymer and a first substituent group bonded to the first atom, a second atom included in each of the plurality of second structural units is bonded to the first atom, and the second atom is different from the first atom, or at least one of all substituent groups on the second atom is different from the first substituent group. 2. The catalyst of claim 1 ,wherein the main chain of the polymer does not include a carbon atom.3. The catalyst of claim 1 ,wherein each of the first atom and the second atom is not a carbon atom.4. The catalyst of claim 1 ,wherein the first atom is a silicon atom.5. The catalyst of claim 1 ,wherein the second atom is an oxygen atom or a nitrogen atom.6. The catalyst of claim 1 ,wherein the metal is any one of selected from the group consisting of palladium, platinum, ruthenium, rhodium, silver, gold, copper, nickel, cobalt, iron, chromium, manganese, technetium, osmium, molybdenum, tungsten, iridium, rhenium, titanium, zirconium, hafnium, tantalum, niobium, and vanadium.7. The catalyst of claim 1 , the first atom is a silicon atom; and', 'the first substituent group is at least any one selected from the group consisting of a substituent group constituted only of a hydrogen atom, a substituent group including an oxygen atom, and a substituent group including a carbon atom., 'wherein8. The catalyst of claim 1 , further comprising an inorganic member or an organic member.9. The catalyst of claim 1 , further ...

PHOSPHINE LIGANDS FOR CATALYTIC REACTIONS

The disclosure is directed to: (a) phosphacycle ligands; (b) methods of using such phosphacycle ligands in bond forming reactions; and (c) methods of preparing phosphacycle ligands. 149-. (canceled)53. The compound of claim 52 , wherein X is attached to an atom of Aradjacent to the atom bonded to Ar.58. The compound according to claim 57 , wherein X comprises a 4-membered ring.59. The compound according to claim 57 , wherein X comprises a 5-membered ring.60. The compound according to claim 57 , wherein X comprises a 7-membered ring or an 8-membered ring.61. The compound according to claim 57 , wherein R claim 57 , R claim 57 , R claim 57 , and Rare selected from the group consisting of alkyl claim 57 , phenyl claim 57 , and heteroaryl claim 57 , or wherein Ror Rtogether with Ror Rform a ring.64. The compound of claim 63 , wherein the compound is selected from the group consisting of:1-(biphenyl-2-yl)-2,2,7,7-tetramethylphosphepan-4-one;1-(biphenyl-2-yl)-2,2,7,7-tetramethylphosphepane;2,2,7,7-tetramethyl-1-(2′,4′,6′-triisopropylbiphenyl-2-yl)phosphepan-4-one;2,2,7,7-tetramethyl-1-(2′,4′,6′-triisopropylbiphenyl-2-yl)phosphepane;2,2,8,8-tetramethyl-1-(2′,4′,6′-triisopropylbiphenyl-2-yl)phosphocan-4-one; and2,2,8,8-tetramethyl-1-(2′,4′,6′-triisopropylbiphenyl-2-yl)phosphocane.67. The compound of claim 66 , wherein the compound is selected from the group consisting of:{'sup': '3,7', '1,3,5,7-tetramethyl-8-(2′,4′,6′-triisopropylbiphenyl-2-yl)-2,4,6-trioxa-8-phosphatricyclo[3.3.1.1]decane; and'}{'sup': '3,7', '8-(biphenyl-2-yl)-1,3,5,7-tetramethyl-2,4,6-trioxa-8-phosphatricyclo[3.3.1.1]decane.'}68. 1-(2-(2 claim 66 ,2 claim 66 ,6 claim 66 ,6-tetramethylphosphinan-1 -yl)phenyl)-1H-pyrrole.71. The compound according claim 69 , wherein ring A is a 4- claim 69 , 5- claim 69 , 6- claim 69 , 7- claim 69 , or 8-membered ring claim 69 , and wherein each of the ring atoms in addition to the phosphorus and 2 carbon ring atoms of formula (Ia) are carbon.72. The compound according to ...

CATALYST SYSTEMS USEFUL IN DEHYDROGENATION REACTIONS

The present disclosure relates to catalyst systems which may be useful for the dehydrogenation of hydrocarbons. According to one or more embodiments, the catalyst systems may include a zincosilicate support material, one or more alkali or alkaline earth metals, and one or more platinum group metals. The zincosilicate support material may include an MFI framework type structure incorporating at least silicon and zinc. The present disclosure also relates to methods for the production of such catalyst systems as well as methods for the use of such catalyst systems for the dehydration of hydrocarbons. 1. A catalyst system useful for the dehydrogenation of hydrocarbons , the catalyst system comprising:a zincosilicate support material comprising an MFI framework type structure incorporating at least silicon and zinc;one or more alkali or alkaline earth metals; andone or more platinum group metals.2. The catalyst system of claim 1 , wherein the molar ratio of zinc to silicon in the MFI framework type structure is from 1:30 to 1:5.3. The catalyst system of claim 1 , wherein the zincosilicate support material comprises at least 95 wt. % of silicon claim 1 , zinc claim 1 , and oxygen in its framework structure.4. The catalyst system of claim 1 , wherein the one or more alkali or alkaline earth metals are selected from K claim 1 , Na claim 1 , or Cs.5. The catalyst system of claim 1 , wherein the catalyst system comprises the alkali or alkaline earth metals in a total amount of from 0.1 wt. % to 3 wt. % of the catalyst system.6. The catalyst system of claim 1 , wherein at least a portion of the one or more alkali or alkaline earth metals are present in elemental form.7. The catalyst system of claim 1 , wherein the one or more platinum group metals are selected from Ru claim 1 , Rh claim 1 , Pd claim 1 , Ir claim 1 , or Pt.8. The catalyst system of claim 1 , wherein the catalyst system comprises the one or more platinum group metals in a total amount of from 0.1 wt. % to 1 wt. ...

METHODS FOR DEHYDROGENATING REACTANT HYDROCARBONS

According to one or more embodiments presently disclosed, one or more reactant hydrocarbons may be dehydrogenated by a method that includes contacting the one or more reactant hydrocarbons with a catalyst system to dehydrogenate at least a portion of the reactant hydrocarbons. The catalyst system may include a zincosilicate support material that includes an MFI framework type structure incorporating at least silicon and zinc. The catalyst system may further include one or more alkali or alkaline earth metals, and one or more platinum group metals. 1. A method for dehydrogenating one or more reactant hydrocarbons , the method comprising: a zincosilicate support material comprising an MFI framework type structure incorporating at least silicon and zinc;', 'one or more alkali or alkaline earth metals; and', 'one or more platinum group metals., 'contacting the one or more reactant hydrocarbons with a catalyst system to dehydrogenate at least a portion of the reactant hydrocarbons, the catalyst system comprising2. The method of claim 1 , wherein the reactant hydrocarbons comprise one or more of n-butane claim 1 , n-pentane claim 1 , or n-hexane.3. The method of claim 2 , wherein the method for dehydrogenating the reactant hydrocarbons results in a selectivity of n-butene claim 2 , n-pentene claim 2 , or n-hexene of at least 30 mol. %.4. The method of claim 2 , wherein the method for dehydrogenating the reactant hydrocarbons results in a yield of n-butene claim 2 , n-pentene claim 2 , or n-hexane of at least 20 mol. %.5. The method of claim 1 , wherein the reactant hydrocarbons are mixed with a diluent claim 1 , the diluent comprising hydrogen claim 1 , steam claim 1 , methane claim 1 , argon claim 1 , nitrogen claim 1 , or mixtures thereof.6. The method of claim 5 , wherein the diluent comprises from 5 vol. % to 30 vol. % of hydrogen.7. The method of claim 1 , wherein the molar ratio of zinc to silicon in the MFI framework type structure is from 1:30 to 1:5.8. The method ...

NOVEL CATALYST SUPPORTS - COMPOSITION AND PROCESS OF MANUFACTURE

A catalyst support comprising at least 95% silicon carbide, having surface areas of ≤10 m/g and pore volumes of ≤1 cc/g. A method of producing a catalyst support, the method including mixing SiC particles of 0.1-20 microns, SiOand carbonaceous materials to form an extrusion, under inert atmospheres, heating the extrusion at temperatures of greater than 1400° C., and removing residual carbon from the heated support under temperatures below 1000° C. A catalyst on a carrier, comprising a carrier support having at least about 95% SiC, with a silver solution impregnated thereon comprising silver oxide, ethylenediamine, oxalic acid, monoethanolamine and cesium hydroxide. A process for oxidation reactions (e.g., for the production of ethylene oxide, or oxidation reactions using propane or methane), or for endothermic reactions (e.g., dehydrogenation of paraffins, of ethyl benzene, or cracking and hydrocracking hydrocarbons). 1. A process for an endothermic reaction , the process comprising reactants over a catalyst support comprising at least 90% SiC and devoid of a catalyst when formed , the catalyst support being impregnated with a catalyst solution after formation.2. The process of claim 1 , wherein the endothermic reaction is dehydrogenation of one or more paraffins.3. The process of claim 1 , wherein the endothermic reaction is dehydrogenation of ethyl benzene to styrene.4. The process of claim 1 , wherein the endothermic reaction is cracking and hydrocracking of heaver hydrocarbons to lighter ones. The disclosed technology regards a silicon carbide catalyst support or carrier which may be impregnated by a silver catalyst, and when so impregnated is useful in processes such as the selective oxidation of ethylene to ethylene oxide and other selective oxidation reactions, such as oxydehydrogenation of ethane, propane to produce corresponding olefins, nitriles, acids, etc., methane oxidative coupling to make ethylene, propylene, ethane, and other desired products. The ...

Catalytic composition and process for the dehydrogenation of butenes or mixtures of butanes and butenes to give 1,3-butadiene

The present invention relates to a catalytic composition which comprises microspheroidal alumina and an active component containing a mixture comprising Gallium and/or Gallium oxides, Tin and/or Tin oxides, a quantity ranging from 1 ppm to 500 ppm with respect to the total weight of the catalytic composition of platinum and/or platinum oxides, and oxides of alkaline and/or alkaline earth metals.

Palladium-Based Supported Hydrogenation Catalyst, And Preparation Method And Application Thereof

The present invention relates to a palladium-based supported hydrogenation catalyst and a preparation method and application thereof. The catalyst is prepared by the following method: impregnating an AlO-containing carrier with an organic solution containing a bipyridine derivative having hydroxy group, optionally drying followed by impregnating with a mixed solution containing the main active component palladium ions and the auxiliary active component M ions, where M is one selected from Ag, Au, Ni, Pb and Cu; and then optionally drying, and calcining to obtain the catalyst. The preparation method provided by the present invention allows Pd atoms and M atoms to be highly uniformly dispersed on the carrier, which overcomes the adverse impact of the surface tension of the impregnation solution and the solvation effect on the dispersibility of active components. The palladium-based supported hydrogenation catalyst provided by the present invention has excellent hydrogenation activity, ethylene selectivity and anti-coking performance, and can be used in a selective hydrogenation process of C2 fraction. 1. A method of preparing a palladium-based supported hydrogenation catalyst , comprising:{'sub': 2', '3, 'impregnating an AlO-containing carrier with an organic solution containing a bipyridine derivative having hydroxy group;'}optionally drying followed by impregnating with a mixed solution containing the main active component palladium ions and the auxiliary active component Mn+ ions, wherein M is selected from one of Ag, Au, Ni, Pb and Cu; andoptionally drying, and calcining to obtain the palladium-based supported hydrogenation catalyst.2. The method according to claim 1 , wherein the impregnation of the AlO-containing carrier with the organic solution containing a bipyridine derivative having hydroxy group is carried out at 20-60° C. claim 1 , and the impregnation duration is 2 to 24 hours.3. The method according to claim 1 , wherein the impregnation of the hydroxy- ...

DEHYDROGENATION CATALYST WITH OPTIMUM MODIFIER PROFILE INDEX

Catalysts and processes for a selective conversion of hydrocarbons. The catalyst comprises: a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a modifier selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof; and a support forming a catalyst particle comprising a plurality of pores. The catalyst has a modifier profile index in a range of 1 to 1.4 across the catalyst particle. 1. A catalyst for a selective conversion of hydrocarbons , the catalyst comprising:a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a modifier selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof; anda support forming a catalyst particle comprising a plurality of pores,wherein the catalyst has a modifier profile index in a range of 1 to 1.4 across the catalyst particle.2. The catalyst of wherein the modifier profile index is in a range of 1 to 1.2.3. The catalyst of wherein the modifier profile index is in a range of 1 to 1.1.4. The catalyst of wherein the first component is platinum claim 1 , the modifier is potassium claim 1 , and the third component is tin.5. The catalyst of wherein the support is selected from the group consisting of silica claim 1 , alumina claim 1 , silica-alumina claim 1 , a zeolite claim 1 , a non-zeolitic molecular sieve claim 1 , titania claim 1 , zirconia and mixtures thereof.6. The catalyst of wherein the catalyst particle is spherical.7. A process for the selective conversion of hydrocarbons claim 1 , the process comprising: a first component selected from the group consisting of Group VIII noble metals and mixtures ...

PROCESS FOR THE SELECTIVE HYDROGENATION OF ACETYLENE TO ETHYLENE

A selective hydrogenation process is described. The process includes dissolving acetylene and hydrogen in a solvent to form a liquid feedstream. The solvent comprises a mixture of a polar organic solvent and a non-polar organic solvent. The liquid feedstream is contacted with a heterogeneous supported selective hydrogenation catalyst at selective hydrogenation conditions to convert at least a portion of the acetylene to ethylene forming a liquid reaction mixture comprising the ethylene produced. 1. A selective hydrogenation process comprising:dissolving acetylene and hydrogen in a solvent to form a liquid feedstream, the solvent comprising a mixture of a polar organic solvent and a non-polar organic solvent; andcontacting the liquid feedstream with a heterogeneous supported selective hydrogenation catalyst at selective hydrogenation conditions to convert at least a portion of the acetylene to ethylene forming a liquid reaction mixture comprising the ethylene produced.2. The process of further comprising separating the ethylene produced from the liquid reaction mixture.3. The process of wherein separating the ethylene produced from the liquid reaction mixture comprises at least one of reducing the pressure claim 2 , and increasing the temperature.4. The process of wherein the polar organic solvent is selected from N-methyl-2-pyrrolidone claim 1 , dimethylformamide claim 1 , acetone claim 1 , tetrahydrofuran claim 1 , dimethylsulfoxide claim 1 , and monomethylamine claim 1 , acetonitrile claim 1 , or combinations thereof.5. The process of wherein the non-polar organic solvent is selected from monoalkyl substituted aromatics claim 1 , dialkyl substituted aromatics claim 1 , trialkyl substituted aromatics claim 1 , and paraffins and wherein the non-polar organic solvent has a boiling point of at least about 100° C.6. The process of wherein the non-polar organic solvent is selected from diethylbenzenes claim 1 , xylenes claim 1 , cumene claim 1 , mesitylene claim 1 , ...

ZEOLITIC MATERIALS HAVING ENCAPSULATED BIMETALLIC CLUSTERS

Zeolites having highly dispersed bimetallic clusters, uniformly distributed in size and composition, encapsulated therein are disclosed. Metal encapsulation and alloying is conferred by introducing ligated metal cation precursors into zeolite synthesis gels, which are subsequently crystallized hydrothermally to form zeolites with metal cations occluded in the pores. The ligated cations are anchored to the zeolite framework via siloxane bridges which enforces their uniform dispersion throughout the zeolite crystals. Treatment of the crystallized zeolites in Oand then Hforms bimetallic clusters, which remain narrowly distributed in size and composition. 1. An aluminosilicate zeolite having an alloyed bimetallic cluster encapsulated in the pores of the aluminosilicate zeolite.2. The aluminosilicate zeolite of claim 1 , wherein the aluminosilicate zeolite is a small pore zeolite having a CHA claim 1 , ERI claim 1 , GIS claim 1 , KFI claim 1 , LEV claim 1 , LTA claim 1 , RTH claim 1 , or SOD framework type.3. The aluminosilicate zeolite of claim 2 , wherein the small pore zeolite has the framework type LTA.4. The aluminosilicate zeolite of claim 1 , wherein the aluminosilicate zeolite is a medium pore zeolite having an EUO claim 1 , FER claim 1 , HEU claim 1 , MEL claim 1 , MFI claim 1 , MFS claim 1 , MTT claim 1 , MTW claim 1 , or TON framework type.5. The aluminosilicate zeolite of claim 1 , wherein the alloyed bimetallic cluster has a dispersity index of 1 to 1.5.6. The aluminosilicate zeolite of claim 1 , wherein the alloyed bimetallic cluster has a surface weighted mean cluster diameter d of 1.0 to 2.0 nm.7. The aluminosilicate zeolite of claim 1 , wherein metals in the alloyed bimetallic cluster are selected from Groups 8 to 12 of the Periodic Table.8. The aluminosilicate zeolite of claim 7 , wherein a collective amount of metals of Groups 8 to 12 is from 0.1 to 5.0 wt. % of the total weight of composite.9. The composition of claim 1 , wherein the alloyed ...

Process for the selective hydrogenation of acetylene to ethylene

A process for a liquid phase selective hydrogenation of acetylene to ethylene in a reaction zone in which acetylene is contacted with hydrogen under hydrogenation conditions and a molar ratio of hydrogen to acetylene in the reaction zone is at least 5, preferably at least 9. A molar ratio of hydrogen to carbon monoxide is preferably approximately 10. The acetylene is preferably absorbed in a solvent.

CNT SHEET SUBSTRATES AND TRANSITION METALS DEPOSITED ON SAME

The present subject matter relates generally to the derivatization of highly-aligned carbon nanotube sheet substrates with one or more transition metal centers and to uses of the resulting metal-derivatized CNT sheet substrates. 1. A CNT sheet or CNT substrate derivatized with one or more metal centers selected from the group of Cu , Pt , Ru , Ti , Pd , Sn , Ag , Au , CuO , CuO , TiO , PdO , SnO , AgO , AuO , Ag/Ti , Pt/Ru , Ag/TiO , Sn/TiO , Pt/TiO , Au/TiO , and Pt/AlO.2. The CNT sheet or CNT substrate of wherein said one or more metal centers comprises one or more of Cu claim 1 , Pt claim 1 , Ti claim 1 , Pd claim 1 , Ag claim 1 , Au claim 1 , Ag/Ti and Pt/Ru.3. The CNT sheet or CNT substrate of wherein said one or more metal centers comprises one or more of Cu claim 2 , Ti claim 2 , Pt claim 2 , Ag claim 2 , and Au.4. The CNT sheet or CNT substrate of wherein said one or more metal centers comprises Cu.5. The CNT sheet or CNT substrate of wherein said one or more metal centers comprises one or more of CuO claim 1 , CuO claim 1 , TiO claim 1 , PdO claim 1 , SnO claim 1 , AgO claim 1 , and AuO.6. The CNT sheet or CNT substrate of wherein said one or more metal centers comprises TiO.7. The CNT sheet or CNT substrate of wherein said one or more metal centers comprises one or more of Ag/TiO claim 1 , Sn/TiO claim 1 , Pt/TiO claim 1 , Au/TiO claim 1 , and Pt/AlO.8. The CNT sheet or CNT substrate of wherein said one or more metal centers comprises Ag/TiO.9. A catalyst comprising the CNT sheet or CNT substrate of .10. The catalyst of claim 9 , wherein said catalyst is an electrocatalyst.11. The catalyst of claim 9 , wherein said catalyst is a photoelectrocatalyst.12. A method of converting carbon dioxide to one or more of carbon monoxide claim 1 , methane claim 1 , ethane claim 1 , higher order hydrocarbons or a combination thereof comprising exposing said carbon dioxide to a catalyst comprising the CNT sheet or CNT substrate of .13. A method of preparing a CNT sheet or ...

CIRCULAR ECONOMY METHODS OF PREPARING UNSATURATED COMPOUNDS

Methods of preparing unsaturated compounds or analogs through dehydrogenation of corresponding saturated compounds and/or hydrogenation of aromatic compounds are disclosed. 1. A method of preparing an unsaturated compound , comprising dehydrogenation of a corresponding saturated compound in the presence of a catalyst system under conditions that effect loss of one or more molecules of hydrogen (H) per molecule of the saturated compound.2. The method of claim 1 , wherein said conditions comprise one or more solvents claim 1 , an elevated temperature claim 1 , a stream of nitrogen to purge liberated hydrogen claim 1 , and any combination thereof.3. The method of claim 1 , further comprising adding one or more hydrogen acceptors to the dehydrogenation reaction to consume the hydrogen molecules.4. The method of claim 1 , wherein said catalyst system is selected from the group consisting of heterogeneous catalyst systems claim 1 , homogeneous catalyst systems claim 1 , and combinations thereof.5. The method of claim 4 , wherein said heterogeneous catalyst system is selected from the group consisting of Pd/C claim 4 , Pd/Alumina claim 4 , Pd/CG claim 4 , Pt/C claim 4 , Pt/Alumina claim 4 , Molybdenum Oxide claim 4 , Vanadium Pentoxide claim 4 , Rh/Alumina claim 4 , Ru/AlO claim 4 , Bismuth Molybdate claim 4 , bi-metallic catalyst systems comprising of metal pairs claim 4 , and combinations thereof.6. The method of claim 4 , wherein said homogeneous catalyst system is selected from soluble transition metal salts claim 4 , Pincer-based catalysts claim 4 , and combinations thereof.7. The method of claim 1 , wherein the saturated compound is a straight chain or branched alkane with or without one or more functional groups claim 1 , each optionally substituted.13. The method of claim 12 , wherein said fixed-bed catalyst comprises 5% Pd/C claim 12 , a nitrogen stream is passed through the flower reactor to remove hydrogen molecules formed claim 12 , and the dehydrogenation ...

CATALYST COMPOSITION FOR THE OXIDATIVE COUPLING OF METHANE USING A SILVER PROMOTER

The invention relates to a catalyst composition, suitable for producing ethylene and other commercially high value C hydrocarbons from methane. The composition contains a silver promoted mixed metal catalyst composition comprising at least two rare earth elements and an alkaline rare earth metal element. The catalyst composition has high catalyst activity and enables oxidative coupling of methane reactions to be conducted at a low reactor temperature while retaining sufficient catalyst selectivity. The invention further provides a method for preparing such a catalyst composition and a process for producing C hydrocarbons, using such a catalyst composition. 1. A composition , comprising a catalyst represented by a general formula (I):{'br': None, 'sub': z', 'a', 'b', 'c', 'd', 'X, '(AgAERE1RE2ATO)'}wherein,(i) ‘Ag’ represents silver;(ii) ‘AE’ represents an alkaline earth metal;(iii) ‘RE1’ represents a first rare earth element;(iv) ‘RE2’ represents a second rare earth element; and(v) ‘AT’ represents a third rare earth element ‘RE3’, or a redox agent selected from antimony, tin, nickel, chromium, molybdenum, tungsten; wherein, ‘a’, ‘b’, ‘c’, ‘d’ and ‘z’ represents relative molar ratio; wherein ‘a’ is 1; ‘b’ ranges from about 0.1 to about 10; ‘c’ ranges from about 0.01 to about 10; ‘d’ ranges from 0 to about 10; ‘z’ ranges from about 0.01 to about 1; ‘x’ balances the oxidation state; wherein, the first rare earth element, the second rare earth element and the third rare earth element, are different.2. The composition of claim 1 , wherein the relative molar ratio ‘z’ ranges from about 0.04 to about 0.18.3. The composition of claim 1 , wherein the relative molar ratio ‘a’ is 1 claim 1 , the relative molar ratio ‘b’ is 0.9 claim 1 , the relative molar ratio ‘c’ is 0.7 claim 1 , the relative molar ratio ‘d’ is 0.1 claim 1 , and the relative molar ratio ‘z’ ranges from about 0.043 to about 0.093.4. The composition of claim 1 , wherein the alkaline earth metal ‘AE’ is ...

CATALYST FOR PREPARING CUMENE AND USE THEREOF

Provided is a catalyst for preparing cumene and use thereof. The catalyst provided includes a carrier and an active ingredient. The active ingredient includes: ingredient (1), which is palladium element; and ingredient (2), which is one or more selected from a group consisting of alkali metal elements, alkaline earth metals and molybdenum element. When the catalyst is used for preparing cumene by α-methyl styrene hydrogenation, AMS conversion rate is high, and a product cumene has high selectivity. 1. A catalyst for preparing cumene , comprising a carrier and an active ingredient , wherein the active ingredient comprises:ingredient (1), which is palladium element; andingredient (2), which is one or more selected from a group consisting of alkali metal elements, alkaline earth metal elements and molybdenum element.2. The catalyst according to claim 1 , wherein calculated by element mass claim 1 , a content of ingredient (1) is 0.01-10 g/L claim 1 , preferably 0.05-5 g/L claim 1 , and more preferably 0.1-4 g/L; and/or a content of ingredient (2) is in a range larger than 0 g/L and equal to or smaller than 60 g/L claim 1 , preferably 0.5-5 g/L claim 1 , and more preferably 1.0-3.5 g/L claim 1 , wherein g/L represents ingredient mass loaded in one liter of carrier.3. The catalyst according to claim 1 , wherein a mass ratio of ingredient (1) to ingredient (2) is in a range of (20-1):1 claim 1 , preferably (15-5):1 claim 1 , and more preferably (12-8):1.4. The catalyst according to claim 1 , wherein ingredient (2) is molybdenum element claim 1 , oringredient (2) comprises an alkali metal element and molybdenum element, wherein preferably, calculated by element mass, a mass ratio of the alkali metal element to the molybdenum element is in a range of (0.1-10):1, preferably (0.2-5):1, more preferably (0.25-4), and most preferably (1-4):1, such as 1:1, 1.5:1, 2:1, 3:1, or 4:1; oringredient (2) comprises an alkaline earth metal element and molybdenum element, wherein ...

CIRCULAR ECONOMY METHODS OF PREPARING UNSATURATED COMPOUNDS

Methods of preparing unsaturated compounds or analogs through dehydrogenation of corresponding saturated compounds and/or hydrogenation of aromatic compounds are disclosed. 2. The method of claim 1 , wherein said conditions comprise one or more solvents claim 1 , an elevated temperature claim 1 , a stream of nitrogen to purge liberated hydrogen claim 1 , and any combination thereof.3. The method of claim 1 , further comprising adding one or more hydrogen acceptors to the dehydrogenation reaction to consume the hydrogen molecules.7. The method of claim 6 , wherein said fixed-bed catalyst comprises 5% Pd/C claim 6 , a nitrogen stream is passed through the flower reactor to remove hydrogen molecules formed claim 6 , and the dehydrogenation reaction is combined with selective hydrogenation of PMI to form 1 claim 6 ,1 claim 6 ,2 claim 6 ,3 claim 6 ,3-pentamethyl-4 claim 6 ,5 claim 6 ,6 claim 6 ,7-tetrahydro-1H-indane (THPMI).8. The method of claim 1 , wherein dehydrogenation is performed in a flow reactor in the presence of a fixed-bed catalyst.9. The method of claim 8 , wherein said fixed-bed catalyst is selected from the group consisting of Pd/C claim 8 , Pd/alumina claim 8 , Pd/Silica claim 8 , Pd/CG claim 8 , Pt/C claim 8 , Pt/alumina claim 8 , molybdenum oxide claim 8 , vanadium pentoxide claim 8 , Rh/alumina claim 8 , Ru/Al2O3 claim 8 , bismuth molybdate claim 8 , and bi-metallic catalyst systems comprising of metal pairs claim 8 , and combinations thereof.11. The method of claim 10 , wherein said catalyst is a fixed-bed catalyst claim 10 , and the hydrogenation is conducted in a flow reactor.12. The method of claim 10 , wherein the hydrogenation reaction is combined with dehydrogenation reaction and a continuous separation process to separate product from the starting material. This application is a divisional of U.S. Ser. No. 15/624,749 filed Jun. 16, 2017, which claims priority to U.S. Application, Ser. No. 62/351,062, filed on Jun. 16, 2016, the contents of ...

Catalyseurs au fer pour l'hydrogénation de l'oxyde de carbone avec une tsheur élevée en hydrocarbure du genre essence

Sulfur terminated organosilica materials and uses thereof

Provided herein are compositions and methods for use of an organosilica material comprising a copolymer of at least one monomer of Formula [R1R2SiCH2]3 (I), wherein, R1 represents a C1-C4 alkoxy group; and R2 is a C1-C4 alkoxy group or a C1-C4 alkyl group; and at least one other monomer of Formula [(Z1O)xZ23-xSi—Z3—SZ4] (II), wherein, Z1 represents a hydrolysable functional group; Z2 represents a C1-C10 alkyl or aryl group; Z3 represents a C2-C11 cyclic or linear hydrocarbon; Z4 is either H or O3H; and x represents any one of integers 1, 2, and 3. The composition may be used as a support material to covalently attach transition metal cations, as a sorbent for olefin/paraffin separations, as a catalyst support for hydrogenation reactions, as a precursor for highly dispersed metal nanoparticles, or as a polar sorbent for crude feeds.

Hydrocarbon hydrogenation catalyst and process

Iron carbon monoxide hydrogenation catalysts

Selective hydrogenation process and catalyst thereof

Catalyst composition, method for its production and its use in the production of hydrocarbons from synthesis gas

A catalyst composition for use in the production of hydrocarbons from synthesis gas comprises the essential metals (a) at least one of iron, cobalt, nickel and ruthenium, and (b) at least one of lithium, sodium, potassium, calcium and magnesium supported on silicate, as described and claimed in US Patent No. 4,061,724, the metals [(a)+(b)] being present on the silicalite support in an amount in the range from 0.5 to 15% by weight. The catalyst composition may be modified by addition of the hydrogen form of a crystalline zeolite having the composition expressed as mole ratios of oxides: wherein M is at least one cation, n is the valence thereof, W is aluminium and/or gallium, Y is silicon and/or germanium and z has a value of 0 to 40, said zeolite being characterised by an XRD pattern which is substantially that of an MFI-type zeolite. Synthesis gas is converted to olefinic hydrocarbons using the unmodified catalyst and to gasoline range hydrocarbons using the modified catalyst.

Catalyst for converting synthesis gas to liquid motor fuels

The addition of an inert metal component, such as gold, silver or copper, to a Fischer-Tropsch catalyst comprising cobalt enables said catalyst to convert synthesis gas to liquid motor fuels at about 240°-370° C. with advantageously reduced selectivity of said cobalt for methane in said conversion. The catalyst composition can advantageously include a support component, such as a molecular sieve, co-catalyst/support component or a combination of such support components.

Catalyst and process for converting synthesis gas to liquid motor fuels

The addition of an inert metal component, such as gold, silver or copper, to a Fischer-Tropsch catalyst comprising cobalt enables said catalyst to convert synthesis gas to liquid motor fuels at about 240°-370° C. with advantageously reduced selectivity of said cobalt for methane in said conversion. The catalyst composition can advantageously include a support component, such as a molecular sieve, co-catalyst/support component or a combination of such support components.

Preparation and use of supported potassium (or rubidium)-Group VIII-metal cluster catalysts in CO/H2 Fischer-Tropsch synthesis reactions

This invention relates to unique supported potassium (or rubidium)-Group VIII-metal cluster catalysts which are useful in CO/H 2 reactions (Fischer-Tropsch synthesis reactions). The novel catalysts of the instant invention are prepared by depositing well characterized potassium (or rubidium)-Group VIII-metal carbonyl cluster complexes onto high surface area supports. Following a subsequent reduction, the precursor bimetallic cluster complexes are decomposed on the support surface forming a potassium (or rubidium) promoted Group VIII-metal cluster catalyst in which the potassium (or rubidium) and Group VIII metals are intimately associated. These unique, highly promoted cluster catalysts have been found to demonstrate high Group VIII-metal dispersions and enhanced Fischer-Tropsch activities and selectivities for producing olefinic and paraffinic hydrocarbons. In addition methane formation is dramatically reduced over the supported bimetallic cluster catalysts of the instant invention when compared to conventionally prepared supported potassium (or rubidium) promoted Group VIII-metal catalysts.

Catalyst composition, method for its production

A catalyst composition for use in the production of hydrocarbons from synthesis gas comprises the essential metals (a) at least one of iron, cobalt, nickel and ruthenium, and (b) at least one of lithium, sodium, potassium, calcium and magnesium supported on silicate, as described and claimed in U.S. Pat. No. 4,061,724, the metals [(a)+(b)] being present on the silicalite support in an amount in the range from 0.5 to 15% by weight. The catalyst composition may be modified by addition of the hydrogen form of a crystalline zeolite having the composition expressed as mole ratios of oxides: 0.9±0.2 M.sub.2 /.sub.n O:W.sub.2 O.sub.3 :20 to 50 YO.sub.2 :zH.sub.2 O wherein M is at least one cation, n is the valence thereof, W is aluminum and/or gallium, Y is silicon and/or germanium and z has a value of 0 to 40, said zeolite being characterized by an XRD pattern which is substantially that of an MFI-type zeolite. Synthesis gas is converted to olefinic hydrocarbons using the unmodified catalyst and to gasoline range hydrocarbons using the modified catalyst.

Catalyst composition, method for its production and its use in the production of hydrocarbons from synthesis gas

A catalyst composition of use in the production of hydrocarbons from synthesis gas comprises the essential metals (a) at least one of iron, cobalt, nickel and ruthenium, and (b) at least one of lithium, sodium, potassium, calcium and magnesium supported on silicate, as described and claimed in U.S. Pat. No. 4,061,724, the metals [(A)+(b)] being present on the silicalite support in an amount in the range from 0.5 to 15% by weight. The catalyst composition may be modified by addition of the hydrogen form of a crystalline zeolite having the composition expressed as mole ratios of oxides: 0.9±0.2M 2 / n O:W 2 O 3 :20 to 50 YO 2 :zH 2 O wherein M is at least one cation, n is the valence thereof, W is aluminum and/or gallium, Y is silicon and/or germanium and z has a value of 0 to 40, said zeolite being characterized by an XRD pattern which is substantially that of an MFI-type zeolite. Synthesis gas is converted to olefinic hydrocarbons using the unmodified catalyst and to gasoline range hydrocarbons using the modified catalyst.

Procédé pour la production catalytique de composés organiques

Method of producing a catalyst used for synthesizing dimethylether from a synthesis gas containing carbon dioxide

The present invention relates to a catalyst used for producing dimethylether, a method of producing the same, and a method of producing dimethylether using the same. More particularly, the present invention relates to a catalyst used for producing dimethylether comprising a methanol synthesis catalyst produced by adding one or more promoters to a main catalyst comprised of a Cu—Zn—Al metal component and a dehydration catalyst formed by mixing Aluminum Phosphate (AlPO 4 ) with gamma alumina, a method of producing the same, and a method of producing dimethylether using the same, wherein a ratio of the main catalyst to the promoter in the methanol synthesis catalyst is in a range of 99/1 to 95/5, and a mixing ratio of the methanol synthesis catalyst to the dehydration catalyst is in a range of 60/40 to 70/30.

Gel catalysts and process for preparing thereof

A gel composition substantially contained within the pores of a solid material for use as a catalyst or as a catalyst support in dehydrogenation and dehydrocyclization processes.

炭化水素転化触媒の調製法

(57)【要約】本公報は電子出願前の出願データであるた め要約のデータは記録されません。

Catalyst used in refinery and petrochemical plants for hydrogenating hydrocarbon streams in gas or liquid phase comprises hydrogenation-active metal on aluminum oxide support

Catalyst comprises a hydrogenation-active metal on an aluminum oxide support and has a specified X-ray diffractogram. Catalyst comprises a hydrogenation-active metal on an aluminum oxide support and has the following specified X-ray diffractogram: planar distance d (10<-10> m) to relative intensity I/Io: 4.52: 0.05-0.1; 2.85: 0.35-0.45; 2.73: 0.65-0.8; 2.44: 0.45-0.55; 2.31: 0.35-0.45; 2.26: 0.35-0.45; 2.02: 0.45-0.6; 1.91: 0.3-0.4; 1.80: 0.1-0.25; 1.54: 0.25-0.35; 1.51: 0-0.35; 1.49: 0.2-0.3; 1.45: 0.25-0.3; 1.39: 1. The metal is a group 8, 9 or 10 metal, preferably Pt or Pd. The catalyst may also contain a group 11 metal, preferably Cu and/or Ag. An Independent claim is also included for the production of the catalyst comprising treating an Al-containing raw material with water, dilute acid or base, forming a molded body, drying, calcining at 900-1100 deg C, impregnating with a solution containing the metal to be deposited, drying and finishing the molded body.

Catalyst for the selective hydrogenation of acetylenic hydrocarbons and process for its preparation

Die Erfindung betrifft ein Verfahren zur Herstellung eines Katalysators, insbesondere für die selektive Reduktion acetylenischer Verbindungen in Kohlenwasserstoffströmen, wobei: - eine Imprägnierlösung bereitgestellt wird, welche als Lösungsmittel ein Gemisch aus Wasser und zumindest einem mit Wasser mischbaren organischen Lösungsmittel enthält, in welchem zumindest eine Aktivmetallverbindung sowie vorzugsweise zumindest eine Promotormetallverbindung gelöst ist; - ein Träger bereitgestellt wird; - der Träger mit der Imprägnierlösung imprägniert wird; - der imprägnierte Träger kalziniert wird. Als Aktivmetall wird bevorzugt Palladium und als Promotormetall bevorzugt Silber verwendet. Ferner betrifft die Erfindung einen Katalysator, wie er mit dem Verfahren erhalten wird, sowie dessen bevorzugte Verwendung zur selektiven Hydrierung acetylenischer Verbindungen. The invention relates to a process for preparing a catalyst, in particular for the selective reduction of acetylenic compounds in hydrocarbon streams, wherein: an impregnating solution is provided which contains as solvent a mixture of water and at least one water-miscible organic solvent in which at least one active metal compound and preferably at least one promoter metal compound is dissolved; - a carrier is provided; - The carrier is impregnated with the impregnating solution; - The impregnated carrier is calcined. The active metal used is preferably palladium and preferably silver as promoter metal. Furthermore, the invention relates to a catalyst as obtained by the process, as well as its preferred use for the selective hydrogenation of acetylenic compounds.

SYNTHESIS AND REGENERATION ON LINE OF A CATALYST USED IN AUTOTHERMAL OXIDATION.

Un proceso para sintetizar o regenerar un catalizador de oxidación en línea, comprendiendo el catalizador al menos un metal del Grupo 8B y, opcionalmente, al menos un promotor, sobre un soporte, siendo el catalizador utilizado en línea en un proceso en el que un hidrocarburo parafínico o una de sus mezclas se pone en contacto con oxígeno en presencia del catalizador en un reactor de oxidación en condiciones de proceso autotérmico suficientes para preparar una olefina, comprendiendo la síntesis o regeneración coalimentar un compuesto metálico volátil del Grupo 8B y/o un compuesto promotor volátil con el hidrocarburo parafínico y la corriente de alimentación de oxígeno en el reactor de oxidación en condiciones de proceso de ignición o autotérmico. A process for synthesizing or regenerating an in-line oxidation catalyst, the catalyst comprising at least one Group 8B metal and, optionally, at least one promoter, on a support, the catalyst being used in-line in a process in which a hydrocarbon Paraffinic or one of its mixtures is contacted with oxygen in the presence of the catalyst in an oxidation reactor under autothermal process conditions sufficient to prepare an olefin, the synthesis or co-regeneration comprising a volatile metal compound of Group 8B and / or a compound comprising volatile promoter with paraffinic hydrocarbon and oxygen feed stream in the oxidation reactor under ignition or autothermal process conditions.

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Palladium containing hydrogenation catalysts

A composition and a process for using the composition in a selective hydrogenation of a highly unsaturated hydrocarbon such as, for example, an alkyne or diolefin, to a less unsaturated hydrocarbon such as, for example, an alkene or a monoolefin, are disclosed. The composition comprising palladium, a selectivity enhancer and an inorganic support wherein the palladium and selectivity enhancer are each present in a sufficient amount to effect the selective hydrogenation of a highly unsaturated hydrocarbon. Optionally, the composition can comprise silver. Also optionally, the palladium is present as skin distributed on the surface of the support. The composition can further comprise an alkali metal-containing compound such as, for example, potassium fluoride.

Hydrocarbon hydrogenation catalyst composition, a process of treating such catalyst composition, and a process of using such catalyst composition

A process of treating a catalyst composition containing palladium, an inorganic support, and a catalyst component, such as silver and/or a modifier such as alkali metal fluoride, is provided. The process involves contacting a catalyst composition with a first treating agent comprising carbon monoxide under a first treating condition to provide a treated catalyst composition. As an option, such treated catalyst composition can then be contacted with a second treating agent comprising a hydrogen-containing fluid under a second treating condition. The treated catalyst composition can be used in a selective hydrogenation process in which highly unsaturated hydrocarbons such as diolefins and/or alkynes are contacted with such treated catalyst composition in the presence of hydrogen to produce less unsaturated hydrocarbons such as monoolefins.

Hydrogenation catalysts for unsaturated hydrocarbons

A composition and a process for using the composition in a selective hydrogenation of a highly unsaturated hydrocarbon such as, for example, an alkyne or diolefin, to a less unsaturated hydrocarbon such as, for example, an alkene or a monoolefin, are disclosed. The composition comprising palladium, a selectivity enhancer and an inorganic support wherein the palladium and selectivity enhancer are each present in a sufficient amount to effect the selective hydrogenation of a highly unsaturated hydrocarbon. Optionally, the composition can comprise silver. Also optionally, the palladium is present as skin distributed on the surface of the support. The composition can further comprise an alkali metal-containing compounds such as, for example, potassium fluoride.

Renewable engine fuel and method of producing same

The present invention provides high-octane fuel, and a method of producing same. These fuels may be formulated to have a wide range of octane values and energy, and may effectively be used to replace 100 LL aviation fuel (known as AvGas), as well as high-octane, rocket, diesel, turbine engine fuels, as well as two-cycle, spark-ignited engine fuels.

Process for dehydrogenating hydrocarbons and oxygenated hydrocarbons

A continuous process for the dehydrogenation of a hydrocarbon and/or oxygenated hydrocarbon feed, comprising contacting the hydrocarbon and/or oxygenated hydrocarbon feed with a dehydrogenation catalyst at elevated temperature in a reaction zone characterised in that the catalyst is capable of retaining hydrogen and (a) is contacted with a feed to form a dehydrogenated product and hydrogen, at least some of the hydrogen formed being adsorbed by the catalyst and/or reacting therewith to reduce at least part of the catalyst; (b) the dehydrogenated product and any unadsorbed/unreacted hydrogen is removed from the reaction zone; (c) at least some of the adsorbed hydrogen is removed from the catalyst and/or at least some of the reduced catalyst is oxidised; and (d) reusing the catalyst from step (c) in step (a).

Shell catalysts, method for producing the same, and the use thereof

In a coated catalyst having a core and at least one shell surrounding the core, the core is made up of an inert support material, the shell or shells is/are made up of a porous support substance, with the shell being attached physically to the core, and a catalytically active metal selected from the group consisting of the metals of the 10th and 11th groups of the Periodic Table of the Elements is present in finely divided form or a precursor of the catalytically active metal is present in uniformly distributed form in the shell or shells. The coated catalyst of the present invention is suitable for the reduction of unsaturated hydrocarbons. Here, better selectivities than in the case of previously known coated catalysts can be achieved. A process for producing the coated catalyst is also described.

Werkwijze voor het bereiden van een katalysator.

Schalenkatalysator für die Gasphasenhydrierung

Die Erfindung betrifft einen Schalenkatalysator mit einem Kern und mindestens einer, den Kern umgebenden Schale, wobei der Kern aus einem inerten Trägermaterial aufgebaut ist, die mindestens eine Schale aus einer porösen Trägersubstanz aufgebaut ist, wobei die Schale physikalisch an den Kern angehaftet ist, und in der mindestens einen Schale ein katalytisch aktives Metall, das aus der Gruppe ausgewählt ist, die von den Metallen der 10. und 11. Gruppe des Periodensystems der Elemente gebildet ist, in feinverteilter Form oder eine Vorstufe des katalytisch aktiven Metalls in gleichmäßig verteilter Form enthalten ist. DOLLAR A Der erfindungsgemäße Schalenkatalysator eignet sich zur Reduktion ungesättigter Kohlenwasserstoffe. Dabei können bessere Selektivitäten im Vergleich zu bisher bekannten Schalenkatalysatoren erreicht werden. Ferner wird ein Verfahren zur Herstellung des Schalenkatalysators beschrieben.

Single-step method of producing butadiene

FIELD: chemistry. SUBSTANCE: invention relates to a single-step method for gas-phase production of butadiene, involving conversion of ethanol or a mixture ethanol and acetaldehyde in the presence of a catalyst, characterised by that the reaction takes place in the presence of a solid-phase catalyst containing a metal selected from: silver, gold or copper, and a metal oxide selected from magnesium, titanium, zirconium, tantalum or niobium oxide. EFFECT: method provides high output of butadiene, selectivity of the process and high degree of conversion of material. 6 cl, 23 ex, 1 tbl РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 440 962 (13) C1 (51) МПК C07C C07C B01J B01J B01J B01J ФЕДЕРАЛЬНАЯ СЛУЖБА B01J ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ B01J (12) ОПИСАНИЕ 11/167 (2006.01) 1/20 (2006.01) 23/54 (2006.01) 23/58 (2006.01) 23/648 (2006.01) 23/76 (2006.01) 23/78 (2006.01) 23/847 (2006.01) ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2010131711/04, 29.07.2010 (24) Дата начала отсчета срока действия патента: 29.07.2010 (73) Патентообладатель(и): Общество с ограниченной ответственностью "УНИСИТ" (ООО "УНИСИТ") (RU) (45) Опубликовано: 27.01.2012 Бюл. № 3 2 4 4 0 9 6 2 (56) Список документов, цитированных в отчете о поиске: JP 57102822 А, 26.06.1982. GB 573631 A, 29.11.1945. US 2374433 A, 24.04.1945. SU 68428 A1, 01.01.1947. (57) Реферат: Изобретение относится к одностадийному способу газофазного получения бутадиена, включающему превращение этанола или смеси этанола с ацетальдегидом в присутствии катализатора, характеризующемуся тем, что взаимодействие проводят в присутствии твердофазного катализатора, содержащего металл, выбранный из группы: серебро, золото или медь, и оксид металла, выбранный из группы оксид магния, титана, циркония, тантала или ниобия. Способ позволяет обеспечить высокий выход бутадиена, селективность процесса и высокую степень конверсии сырья. 5 з.п. ф-лы, 1 табл. R U 2 4 4 0 9 6 2 (54) ОДНОСТАДИЙНЫЙ СПОСОБ ПОЛУЧЕНИЯ БУТАДИЕНА Ñòð.: 1 C 1 C 1 Адрес для переписки: 119991, ...

Regeneration of dehydrogenation catalyst of alkane with oxychlorination with low content of chlorine

FIELD: chemical or physical processes.SUBSTANCE: invention relates to a method of reducing time for exposure treatment in air during regeneration, including (i) removing surface carbon compounds from a gallium dehydrogenation catalyst of the alkane during burning in the presence of fuel gas, (ii) conditioning the gallium dehydrogenation catalyst of the alkane after step (i) by treatment in air at temperature of 660 degrees Celsius (°C) to 850 °C with (iii) oxygen-containing gas stream, containing (iv) from 0.1 to 100 parts per million by volume (ppm) of a chlorine source selected from chlorine, a chlorine compound or a combination thereof, and achieving a predetermined percentage of alkane conversion for the gallium dehydrogenation catalyst subjected to the regeneration process, including exposure on air using steps from (i) to (iv), by 10 to 50 % faster when treated with exposure on air, than required to achieve the same pre-specified percentage conversion of the alkane for the gallium dehydrogenation catalyst subjected to the regeneration process, including exposure on air using steps from (i) to (iii), but without (iv).EFFECT: technical result consists in increase in efficiency and efficiency of alkane dehydrogenation.10 cl, 2 tbl, 1 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) (19) RU (11) (13) 2 724 336 C2 (51) МПК B01J 38/44 (2006.01) B01J 38/34 (2006.01) B01J 23/62 (2006.01) B01J 23/08 (2006.01) B01J 38/18 (2006.01) B01J 38/30 (2006.01) C07C 5/32 (2006.01) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 38/44 (2020.02); B01J 38/34 (2020.02); B01J 23/62 (2020.02); B01J 23/08 (2020.02); B01J 38/18 (2020.02); B01J 38/30 (2020.02); C07C 5/32 (2020.02) (21)(22) Заявка: 2018132833, 22.02.2017 22.02.2017 Дата регистрации: Приоритет(ы): (30) Конвенционный приоритет: 01.03.2016 US 62/301,856 (43) Дата публикации заявки: 17.03.2020 Бюл. № 8 (45) Опубликовано: 23.06.2020 Бюл. № 18 (86) Заявка PCT: US 2017/018902 (22.02.2017) C 2 C 2 ( ...

CATALYST FOR SELECTIVE HYDROGENATION OF ACETYLENE WITH SEGREGATED PALADY SKIN AND METHOD FOR TREATMENT OF GASEOUS BLENDS CONTAINING IT

Reivindicación 1: Un catalizador para la hidrogenación selectiva del acetileno que comprende; un soporte seleccionado del grupo de : alúmina, titanio, zirconio, aluminato de zinc, titanato de zinc y mezclas de estos, donde el soporte posee una superficie externa uniformemente redondeada, un área de superficie en el rango de aproximadamente 3 a 10 metros cuadrados por gramo, y un volumen de poro aproximadamente de 0,24 a 0,64 centímetros cúbicos por gramo. Paladio en un rango de 0,01 a 1,0% en peso del catalizador, donde sustancialmente todo el paladio está concentrado en la piel periférica del catalizador donde la piel periférica posee un grosor de aproximadamente 400 micrones; y Plata en el rango de 0,5 a 10,0 veces el peso del paladio donde la plata se encuentra distribuida a través de todo el catalizador. Reivindicación 19: Un método para el tratamiento de mezclas gaseosas que contienen acetileno, caracterizado porque el método involucra la hidrogenación selectiva del acetileno, poniendo en contacto la mezcla junto con el hidrógeno con el catalizador de acuerdo con cualquiera de las reivindicaciones precedentes. Claim 1: A catalyst for the selective hydrogenation of acetylene comprising; a support selected from the group of: alumina, titanium, zirconium, zinc aluminate, zinc titanate and mixtures thereof, where the support has a uniformly rounded outer surface, a surface area in the range of approximately 3 to 10 square meters per gram, and a pore volume of approximately 0.24 to 0.64 cubic centimeters per gram. Palladium in a range of 0.01 to 1.0% by weight of the catalyst, where substantially all of the palladium is concentrated in the peripheral skin of the catalyst where the peripheral skin is approximately 400 microns thick; and Silver in the range of 0.5 to 10.0 times the weight of palladium where silver is distributed throughout the catalyst. Claim 19: A method for the treatment of gaseous mixtures containing acetylene, characterized in that the method ...

Palladium-based catalyst for selective hydrogenation of acetylene

본 발명은 아세틸렌의 에틸렌으로의 선택적 수소화에 있어서, 낮은 온도에서 환원된 후에도 높은 에틸렌 선택도를 갖는, La, Ti, Nb, K 또는 Si를 추가로 포함하는 Pd-촉매에 관한 것이다. 본 발명의 촉매는 필수적으로 지지 촉매를 기준으로 0.05 내지 2.0 중량%의 팔라듐, 및 란탄, 니오브, 티타늄, 칼륨 및 규소로 이루어진 군에서 선택된 1종 또는 2종의 금속으로 이루어진다. 이러한 촉매를 다음 방법으로 제조한다: (1) 테트라아민 팔라듐 수산화물 수용액에 지지체를 함침시키고, 건조시키고, 하소시키고, (2) Pd-촉매를 금속 전구체의 용액에 함침시키고, 건조시키고, 하소시켜서 제2, 및 필요하다면 제3의 금속을 함침시키고, (3) 단계 (2)에 따른 촉매를 수소 중에서 200 내지 600 ℃에서 1 내지 5 시간 동안 환원시킨다. The present invention relates to a Pd-catalyst further comprising La, Ti, Nb, K or Si, in the selective hydrogenation of acetylene to ethylene, having high ethylene selectivity even after being reduced at low temperatures. The catalyst of the present invention consists essentially of 0.05 to 2.0% by weight of palladium, based on the supported catalyst, and one or two metals selected from the group consisting of lanthanum, niobium, titanium, potassium and silicon. These catalysts are prepared by the following methods: (1) impregnating, drying and calcining the support in aqueous tetraamine palladium hydroxide solution, and (2) impregnating the Pd-catalyst in a solution of the metal precursor, drying and calcining 2, and if necessary, a third metal, and (3) the catalyst according to step (2) is reduced in hydrogen at 200 to 600 ° C. for 1 to 5 hours. 선택적 수소화, 팔라듐 촉매, 에틸렌 선택도 Selective Hydrogenation, Palladium Catalyst, Ethylene Selectivity

A catalyst for selective hydrogenating unsaturated hydrocarbon, and a preparation and an application of the same

본 발명은 불포화 탄화수소의 선택적 수소화를 위한 선택적 수소화 촉매, 이 촉매의 제조 방법 및 그의 용도에 과한 것이다. 본 발명의 촉매는 담체, 활성 성분 Pd, 희토류 금속, 및 보조 금속 Bi, Ag 등을 포함한다. 상기 촉매는 알킨과 같은 고도의 불포화 탄화수소를 고도의 공간속도에서도 고도의 선택성을 가지고, 촉매 상의 그린오일 형성 및 탄소 침적이 매우 낮은 상태에서 수소화할 수 있으며, 이는 산업적 분해 공정에도 매우 유용하다. The present invention is directed to a selective hydrogenation catalyst for the selective hydrogenation of unsaturated hydrocarbons, a process for preparing the catalyst and its use. Catalysts of the present invention include a carrier, active component Pd, rare earth metals, and auxiliary metals Bi, Ag and the like. The catalysts have a high selectivity at high space velocities for highly unsaturated hydrocarbons, such as alkynes, and can be hydrogenated at very low levels of green oil formation and carbon deposition on the catalyst, which is also very useful for industrial cracking processes. 불포화 탄화수소, 올레핀, 수소화, 촉매, 희토류, 알킨 Unsaturated hydrocarbons, olefins, hydrogenation, catalysts, rare earths, alkynes

CATALYTIC SYSTEM

UN AGENTE DE RETENCION DE HIDROGENO QUE CONTIENE UN OXIDO METALICO REDUCIBLE O UN ADSORBEDOR DE HIDROGENO, TENIENDO DICHO AGENTE UN REVESTIMIENTO POROSO. A HYDROGEN RETENTION AGENT CONTAINING A REDUCABLE METAL OXIDE OR A HYDROGEN ADHESOR, HAVING SUCH AGENT A POROUS COATING.

一种选择加氢除炔多金属催化剂

本发明提供了一种选择加氢除炔多金属催化剂。包括以下组份：含量为1-30%wt的Cu，含量为0.001-5%wt的Pd，选自氧化铝、氧化硅或氧化钛中的至少一种载体。此外，还可包括含量为0.001-6%wt且选自铋、锆、铅、银、铂中的一种或多种助剂金属。采用本发明催化剂，碳四馏份的炔含量可降至15ppm以下，1，3-丁二烯损失可小于1.5%wt。

Способ превращения углеводородов

1. Способ превращения углеводородов, включающий следующие стадии: (а) обеспечение первой смеси, включающей ≥0,5 мас.% углеводорода и ≥4,0 мас.част./млн меркаптана, в расчете на массу первой смеси; и (б) воздействие на первую смесь температуры ≥1,20·10°C в первой зоне при условиях пиролиза с целью превращения по меньшей мере части углеводорода и ≥90,0 мас.% меркаптана, содержащегося в первой смеси, в расчете на массу меркаптана в первой смеси, с получением второй смеси, которая включает ≥1,0 мас.% Cненасыщенных углеводородов, ≤20,0 мас.% CO, причем x составляет 1 или 2, и ≤1,0 мас.част./млн тиофена, в расчете на массу второй смеси.2. Способ по п.1, в котором первая смесь включает ≥20,0 мас.% метана и ≥10,0 мас.част./млн метилмеркаптана, в расчете на массу первой смеси; первая смесь получена из природного газа без применения каких-либо промежуточных стадий удаления меркаптана, причем вторая смесь включает ≤0,05 мас.част./млн метилмеркаптана, в расчете на массу второй смеси.3. Способ по п. 1 или 2, в котором первая смесь дополнительно включает сероводород в количестве в интервале от 50,0 мас.част./млн до 5 мас.%, в расчете на массу первой смеси.4. Способ по п. 1 или 2, в котором первую смесь подвергают воздействию температуры ≥1,45·10°C в ходе пиролиза.5. Способ по п. 1 или 2, дополнительно включающий (в) отделение сероводорода от второй смеси с получением третьей смеси.6. Способ по п.5, дополнительно включающий (г) соединение первого и второго реагентов во второй зоне с получением четвертой смеси, первая и вторая зоны по меньшей мере частично совпадают; и (д) по меньшей мере частичное окисление четвертой смеси во второй зоне с получением пятой смеси; причем (1) пиролиз РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (51) МПК C07C 2/76 (13) 2013 136 689 A (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2013136689/04, 20.12.2011 (71) Заявитель(и): ЭКСОНМОБИЛ КЕМИКЭЛ ПЕЙТЕНТС ИНК. (US) Приоритет(ы): (30) Конвенционный ...

Process for producing acetic acid,acetic aldehyde,ethanol and c2-c4 olefins

1. СПОСОБ ПОЛУЧЕНИЯ СМЕСИ УКСУСНОЙ КИСЛОТЫ, УКСУСНОГО АЛЬДЕГИДА , ЭТАНОЛА И Сг - С ОЛЕФИНОВ при мол рном соотношении кислородосодержащих соединений и олефинов, равном 1. A METHOD FOR OBTAINING A MIXTURE OF ACETIC ACID, ACETIC ALDEHYDE, ETHANOL AND Cr - C OLEFINS with a molar ratio of oxygen-containing compounds and olefins equal to

최적의 개질제 프로파일 지수를 갖는 탈수소화 촉매

본 발명은 탄화수소의 선택적 전환을 위한 촉매 및 방법에 관한 것이다. 촉매는 VIII족 귀금속 및 이들의 혼합물로 이루어진 군으로부터 선택되는 제1 성분, 알칼리 금속 또는 알칼리 토금속 및 이들의 혼합물로 이루어진 군으로부터 선택되는 개질제, 및 주석, 게르마늄, 납, 인듐, 갈륨, 탈륨 및 이들의 혼합물로 이루어진 군으로부터 선택되는 제3 성분; 및 복수의 기공을 포함하는 촉매 입자를 형성하는 지지체를 포함한다. 촉매는 개질제 프로파일 지수(profile index)가 촉매 입자를 가로질러 1 내지 1.4의 범위이다.

Catalyst composition for alkene oligomerisation and co-oligomerisation

A catalyst composition comprising a first component which is a substituted bis(cyclopentadienyl)titanium, zirconium or hafnium compound, also containing a substituent which is attached to the metal and which is capable of reacting with a cation and a second component which is a compound having a bulky and labile anion which is substantially non-coordinating under the reaction conditions and a cation, wherein the substituted bis-cyclopentadienyl ligand pair is bis-tetramethylcyclopentadienyl.

Catalyst composition for alkene oligomerisation and co-oligomerisation

본 발명은 금속에 부착되고 양이온과 반응할 수 있는 치환체를 또한 함유하는 치환된-비스(시클로펜타디에닐) 티타늄, 지르코늄 또는 하프늄 화합물인 제 1 성분, 및 반응 조건 하에서 실질적으로 배위하지 않는 부피가 크고 불안정한 음이온 및 양이온을 갖는 화합물인 제 2 성분을 포함하고, 치환된 비스-시클로펜타디에닐 리간드 쌍이 비스-테트라메틸시클로펜타디에닐인 촉매 조성물에 관한 것이다. The present invention relates to a first component which is a substituted-bis (cyclopentadienyl) titanium, zirconium or hafnium compound that also attaches to metals and may contain substituents capable of reacting with cations, and a volume that is substantially uncoordinated under the reaction conditions. It relates to a catalyst composition comprising a second component which is a compound having a large unstable anion and a cation and wherein the substituted bis-cyclopentadienyl ligand pair is bis-tetramethylcyclopentadienyl.

알켄 올리고머화 및 공-올리고머화를 위한 촉매 조성물(catalyst composition for alkene oligomerisation and cooligomerisation)

본 발명은 금속에 부착되고 양이온과 반응할 수 있는 치환체를 또한 함유하는 치환된-비스(시클로펜타디에닐) 티타늄, 지르코늄 또는 하프늄 화합물인 제1성분, 및 반응 조건 하에서 실질적으로 배위하지 않는 부피가 크고 불안정한 음이온 및 양이온을 갖는 화합물인 제2성분을 포함하고, 치환된 비스-시콜로펜타디에닐 리간드 쌍이 비스-데트라메틸시클로펜타디에닐인 촉매 조성물에 관한 것이다.

Hydroisomerisation of butene double bonds

FIELD: chemistry. ^ SUBSTANCE: invention relates to a method of converting a C4 stream, containing 1-butene and 2-butene, preferably into 2-butene, involving: mixture of the said C4 stream with the first hydrogen stream to form the input stream, hydroisomerisation of the said input stream in the presence of first hydroisomerisation catalyst, so as to convert at least part of the said 1-butene to 2-butene and obtain an output hydroisomerisation product, separation of the output hydroisomerisation product in a catalytic distillation column, with a top end and a bottom end, to obtain a mixture of 1-butene at the said top end, a top output stream which contains isobutene and isobutylene, and a bottom stream which contains 2-butene, and hydroisomerisation of the said mixture of 1-butene at the said top end of the catalytic distillation column using a second hydroisomerisation catalyst to obtain additional 2-butene in the said bottom stream; where location of the said second hydroisomerisation catalyst in the top section of the column as a separate reaction zone is chosen to achieve maximum concentration of 1-butene, under the condition that, the hydroisomerisation stage with participation of the second isomerisation catalyst does not take place. The invention also relates to an apparatus for realsing this method and a method of producing propylene from a C4 stream. ^ EFFECT: selective hydrogenation of 1-butene to 2-butene which is more efficient than existing technologies. ^ 30 cl, 7 dwg, 4 tbl, 2 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 370 480 (13) C2 (51) МПК C07C 5/25 (2006.01) C07C 6/04 (2006.01) C07C 11/06 (2006.01) C07C 11/08 (2006.01) B01J 8/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21), (22) Заявка: 2007142195/04, 07.04.2006 (24) Дата начала отсчета срока действия патента: 07.04.2006 (73) Патентообладатель(и): КАТАЛИТИК ДИСТИЛЛЕЙШН ТЕКНОЛОДЖИЗ (US) (43) Дата публикации заявки: ...

Catalyst and method

FIELD: chemistry. SUBSTANCE: invention relates to two versions of method of hydrocarbon dehydration. One of versions contains stage of supplying raw material flow, containing at least one carbohydrate, above catalyst, containing catalytically active carbon phase. Said catalyst is formed by passing hydrocarbon-containing gas above catalyst precursor at temperature within the interval from 650°C to 750°C for at least 5 minutes to form active carbon phase, where said catalyst precursor contains either metal compound, applied on porous carrier or preliminarily formed carbon nanofibrous material, where dehydration is realised in fact in absence of oxygen. EFFECT: claimed invention represents improved version of dehydration method. 9 cl, 8 dwg, 15 tbl, 19 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: (19) RU (11) (13) 2 565 757 C2 (51) МПК C07C 5/32 (2006.01) C07C 5/333 (2006.01) C07C 11/08 (2006.01) C07C 11/167 (2006.01) C07C 11/06 (2006.01) B01J 23/22 (2006.01) B01J 37/08 (2006.01) ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2011153777/04, 04.06.2010 (24) Дата начала отсчета срока действия патента: 04.06.2010 Приоритет(ы): (30) Конвенционный приоритет: (72) Автор(ы): СТИТТ Эдмунд Хью (GB), УОТСОН Майкл Джон (GB), ГЛАДДЕН Линн (GB), МАКГРЕГОР Джеймс (GB) R U (73) Патентообладатель(и): ДЖОНСОН МЭТТИ ПЛС (GB), КЕМБРИДЖ ЭНТЕРПРАЙЗ ЛТД (GB) 05.06.2009 GB 0909694.2; 05.08.2009 GB 0913579.9 (43) Дата публикации заявки: 20.07.2013 Бюл. № 20 2 5 6 5 7 5 7 (45) Опубликовано: 20.10.2015 Бюл. № 29 (56) Список документов, цитированных в отчете о поиске: US 5220092 A, 15.06.1993. EP 0790225 A1, 20.08.1997 . RU 2123993 C1, 27.12.1998 . RU 2005100036 A, 10.06.2005 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 10.01.2012 (86) Заявка PCT: 2 5 6 5 7 5 7 R U C 2 C 2 GB 2010/050944 (04.06.2010) (87) Публикация заявки PCT: WO 2010/140005 (09.12.2010) Адрес для переписки: 129090, Москва, ул. Большая Спасская, 25, стр. 3, ООО " ...

균일형 백금 담지 알루미나 촉매, 그 제조 방법, 및 그 사용 방법

본 발명은 촉매 수명에 있어서 우수한 성능을 갖는 균일형 백금 담지 알루미나 촉매를 제공한다. 해결방법으로서 균일형 백금 담지 알루미나 촉매는 알루미나 담체와, 알루미나 담체의 단면 전체에 걸쳐 분산된 황 또는 황 화합물과, 알루미나 담체의 단면 전체에 걸쳐 분산되어 담지된 백금과, 나트륨, 칼륨, 및 칼슘의 군으로부터 선택되는 1 종 또는 2 종 이상의 알칼리 금속을 갖는다. 백금의 함유량은 백금 원소로서 0.05 이상 5.0wt% 이하이면 된다. 황 또는 황 화합물의 함유량은 황 원소로서 0.15 이상 5.0wt% 이하이면 된다. 알칼리 금속의 함유량은 알칼리 금속 원소로서 0.1wt% 이상 5.0wt% 이하이면 된다.

用于链烯烃低聚与共低聚的催化剂组合物

一种催化剂组合物，其中含有作为第一组分的被取代-二(环戊二烯基)钛、锆或铪化合物，还含有一种连结在金属上并且能够与阳离子反应的组分，作为第二组分的一种化合物，其中具有阳离子和体积庞大且不稳定在反应条件下基本上不配位的阴离子，其特征在于被取代二环戊二烯基配位体对为二-四甲基环戊二烯基。

1,3-부타디엔을 제공하기 위한 부텐 또는 부탄과 부텐의 혼합물의 탈수소화용 촉매 조성물 및 공정

본 발명은 미소구상 알루미나 및 갈륨 및/또는 갈륨 산화물, 주석 및/또는 주석 산화물, 촉매 조성물의 총 중량에 대하여 1 ppm 내지 500 ppm 범위의 양의 백금 및/또는 백금 산화물, 및 알칼리 금속 및/또는 알칼리 토금속의 산화물을 포함하는 혼합물을 함유하는 유효 성분을 포함하는 촉매 조성물에 관한 것이다.

Catalysts

利用有机掺杂剂增强的基于钯的乙炔选择性氢化催化剂

一种组合物，其含有包括钯和载体的负载型氢化催化剂，其中所述负载型氢化催化剂能够将高度不饱和烃选择性地氢化成不饱和烃；以及包括芴或芴酮型结构的掺杂剂。一种制备选择性氢化催化剂的方法包括使载体与含钯化合物接触形成负载型钯组合物；使所述负载型钯组合物与包括芴或芴酮型结构的掺杂剂接触形成选择性氢化催化剂前体；并且还原所述选择性氢化催化剂前体以形成选择性氢化催化剂。一种将高度不饱和烃选择性氢化成富含不饱和烃的组合物的方法，所述方法通过以下方式进行：在适合于氢化至少一部分高度不饱和烃进料的条件下，使包括钯的负载型催化剂和包括芴或芴酮型结构的掺杂剂与包括高度不饱和烃的进料接触，以形成富含不饱和烃的组合物。