WO2019224412A1 - Proceso catalítico para la producción de hidrocarburos y compuestos aromáticos a partir de compuestos oxigenados presentes en mezclas acuosas - Google Patents
Proceso catalítico para la producción de hidrocarburos y compuestos aromáticos a partir de compuestos oxigenados presentes en mezclas acuosas Download PDFInfo
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- WO2019224412A1 WO2019224412A1 PCT/ES2019/070340 ES2019070340W WO2019224412A1 WO 2019224412 A1 WO2019224412 A1 WO 2019224412A1 ES 2019070340 W ES2019070340 W ES 2019070340W WO 2019224412 A1 WO2019224412 A1 WO 2019224412A1
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- QHGNHLZPVBIIPX-UHFFFAOYSA-N tin(ii) oxide Chemical class [Sn]=O QHGNHLZPVBIIPX-UHFFFAOYSA-N 0.000 description 1
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- MWOOGOJBHIARFG-UHFFFAOYSA-N vanillin Chemical compound COC1=CC(C=O)=CC=C1O MWOOGOJBHIARFG-UHFFFAOYSA-N 0.000 description 1
- FGQOOHJZONJGDT-UHFFFAOYSA-N vanillin Natural products COC1=CC(O)=CC(C=O)=C1 FGQOOHJZONJGDT-UHFFFAOYSA-N 0.000 description 1
- 235000012141 vanillin Nutrition 0.000 description 1
- PZSJOBKRSVRODF-UHFFFAOYSA-N vanillin acetate Chemical compound COC1=CC(C=O)=CC=C1OC(C)=O PZSJOBKRSVRODF-UHFFFAOYSA-N 0.000 description 1
- 235000013311 vegetables Nutrition 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/14—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of germanium, tin or lead
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
- B01J21/063—Titanium; Oxides or hydroxides thereof
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/10—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of rare earths
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/20—Vanadium, niobium or tantalum
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/001—Controlling catalytic processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
- C10G3/44—Catalytic treatment characterised by the catalyst used
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/54—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids characterised by the catalytic bed
- C10G3/55—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids characterised by the catalytic bed with moving solid particles, e.g. moving beds
- C10G3/57—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids characterised by the catalytic bed with moving solid particles, e.g. moving beds according to the fluidised bed technique
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/60—Controlling or regulating the processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
- C10G2300/1014—Biomass of vegetal origin
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Definitions
- This invention belongs to the field of the synthesis and application of solid catalysts for the conversion of biomass mainly of the lignocellulosic type and its derivatives into liquid fuels for transport.
- Biomass, together with C0 2 is one of the primary and renewable sources of coal.
- the valorization of biomass (mainly vegetable or lignocellulosic type) and its derivatives is a sustainable alternative to the use of fossil sources for the production of fuels and chemical products, thus reducing the obvious problems of depletion of non-renewable resources and the environmental issues associated with them [GW Huber, S. Iborra, A. Corma. Chemical Reviews, 106 (2006) 4044]
- the co-production of biofuels together with other chemical products of interest is essential.
- aqueous fractions containing mixtures of oxygenated organic compounds can be obtained (ie acids, aldehydes, alcohols, polyols, sugars, furans, phenols, etc.) that are not currently being used [A. Corma, S. Iborra, A. Velty, Chemical Reviews, (2007) 2411]
- pyrolysis oils or bio-liquids can be obtained mostly.
- bio-liquids are complex mixtures of more than 200 components, containing different water proportions and fundamentally oxygenated organic compounds (ie alcohols, ketones, acids, polyalcohols, furans, phenols, among others) of different molecular size that are characterized by their high oxygen content and great reactivity.
- the bio-liquids also have a high acidity due to the presence of short chain carboxylic acids (C1-C4), which makes storage and direct use difficult.
- an organic phase can be obtained, on the one hand, containing various organic compounds of interest for later use as fuels; and on the other hand aqueous fractions and effluents containing C1-C4 short chain carboxylic acids (mainly acetic acid) together with other compounds such as aldehydes, ketones or alcohols and small amounts of furanic compounds and / or heavier compounds, which are not being currently used and constitute residual currents in bio-refineries [M. Asadieraghi et al., Renewable and Sustainable Energy Reviews, 36 (2014) 286, E. E. lojoiu et al., Applied Catalysis A: Gen. 323 (2007) 147]
- C1-C4 short chain carboxylic acids mainly acetic acid
- oxygenated organic compounds mostly short chain ( ⁇ C5) have little value in themselves, but can be efficiently transformed to generate mixtures of longer chain hydrocarbons and aromatic compounds that are very useful as precursors, components and / or additives in automotive liquid fuels.
- These compounds (hydrocarbons and aromatics) are produced by the formation of carbon-carbon bonds through reactions of condensation, ketoneization, alkylation with alcohols, which occur consecutively [CA Gaertner et al. Journal of Catalysis, 266 (2009) 71]
- other reactions such as decarboxylation, dehydration or esterification can occur when treating these complex aqueous mixtures.
- the present invention relates to a catalytic process for the production of mixtures of hydrocarbons and aromatic compounds, which may comprise at least the following steps:
- a catalyst which may contain in its composition at least - Sn and Nb, and combinations of Sn-Nb with other transition metals, rare earths or lanthanides,
- step (c) recover the products obtained in step (b) by a process of liquid / liquid separation of the aqueous and organic phases.
- the process of the present invention for the catalytic condensation of oxygenated organic compounds present in aqueous fractions derived from biomass in mixtures of hydrocarbons and aromatic compounds (preferably C5-C16), can use a catalyst having the empirical formula :
- - M is a chemical element of the group of transition metals, rare earths or lanthanides
- - a is between 0.05 and 10.0
- - b and c are between 0 and 10.0, with c + b other than zero (c + b 1 0)
- - d is between 0 and 4.0
- - e has a value that depends on the oxidation state of the elements Sn, Nb, Ti and the element M.
- the catalyst must comply with the condition that the catalyst comprises at least Sn and Nb and / or Ti, and that, in its calcined form, it is presented as a mixed metal oxide formed mostly by the rutile-like crystalline phase of the Sn0 2 in which at least Nb and / or Ti are incorporated.
- Said catalyst can be prepared by conventional methods from solutions of compounds of the different elements, of solutions of the same pure elements, or of mixing them, with the desired atomic relationships.
- Said solutions are preferably aqueous solutions.
- the catalyst is obtained by a process comprising at least:
- the mixing step can be carried out from the compounds of the different elements, from the pure elements themselves in solution, using co-precipitation methods or by hydrothermal methods.
- the elements Sn, Nb, Ti and the metal M can be incorporated into the mixing stage as pure metal elements, as salts, as oxides, as hydroxides, as alkoxides, or as mixtures of two or more of the aforementioned forms.
- salts sulfates, nitrates, oxalates or halides are preferably used, without these limiting examples.
- the Sn can be incorporated into the mixing stage preferably as tin oxide, tin acetate, tin nitrate, tin chloride, tin fluoride, tin isopropoxide, tin oxalate or tin sulfate.
- the Nb can be incorporated into the mixing step preferably as niobium pentoxide, niobium oxalate, niobium chloride or Nb metal.
- the Ti can be incorporated into the mixing stage preferably as titanium dioxide, titanium oxychloride, titanium oxy sulfate, titanium nitrate, titanium tetrachloride, titanium ethoxide, titanium isopropoxide, titanium butoxide or Ti metal.
- the mixing step can be followed by a period of static permanence in the reactor, or the mixing can be carried out with stirring. Both static permanence and agitation can be performed in a normal reactor or in a autoclave.
- the mixing step can be carried out in solution or by hydrothermal treatment.
- the drying step can be carried out by conventional methods in an oven, evaporation with stirring, evaporation in a rotary evaporator, or vacuum drying.
- the step of calcining the dry solid can be carried out under an inert gas atmosphere, such as nitrogen, helium, argon or mixtures thereof, as well as air or mixtures of air with other gases.
- an inert gas atmosphere such as nitrogen, helium, argon or mixtures thereof, as well as air or mixtures of air with other gases.
- This calcination stage can be carried out by passing a flow of inert gas (with space velocities between 1 and 400 h 1 ) or in static.
- the temperature is preferably in a range between 250 and 850 ° C and more preferably between 400 and 600 ° C.
- the calcination time is not decisive, but it is preferred that it is in a range between 0.5 hours and 20 hours.
- the heating rate is not decisive, but is preferred in a range between 0.1 ° C / minute and 10 ° C / minute.
- the catalyst may also be initially calcined in an oxidizing atmosphere to a temperature between 200 and 350 ° C, and more preferably between 240 and 290 ° C, and subsequently subjected to calcination in an inert atmosphere.
- the catalyst is obtained, as indicated above, by co-precipitation of the elements, either from precursor compounds containing the different elements or from the pure elements themselves in solution.
- precursor compounds containing the elements Sn, Nb, Ti and the element M salts, oxides, hydroxides, alkoxides or mixtures of two or more of the aforementioned forms can be used. Sulfates, nitrates, oxalates or halides are preferably used as salts.
- solvents water, methanol, ethanol, iso-propanol, acetonitrile, dioxane, or mixtures thereof, preferably water, can be used.
- Co-precipitation of the elements in the solution is carried out by controlled change of pH by the addition of a basic compound selected from alkali metal hydroxides, alkaline earth metal hydroxides, ammonium hydroxide or ammonia water, and alkali metal hypochlorites, Without being these limiting examples.
- a basic compound selected from alkali metal hydroxides, alkaline earth metal hydroxides, ammonium hydroxide or ammonia water, and alkali metal hypochlorites, Without being these limiting examples.
- the catalyst is obtained using hydrothermal methods (containing two or more elements in the synthesis, especially containing Sn, Nb, Ti and element M) in which the temperature and synthesis time can be decisive.
- the synthesis temperature is preferably between 100 and 250 ° C and, more preferably, between 150 and 180 ° C.
- the synthesis time is preferably between 6 and 500 hours, and more preferably between 24 and 200 hours.
- the catalyst is obtained by impregnating the precursors containing the elements Nb, Ti and the metal M on a material Sn0 2, presenting mostly the rutile crystalline phase.
- precursor compounds containing elements Nb, Ti and element M salts, oxides, hydroxides, alkoxides or mixtures of two or more of the aforementioned forms can be used. Sulfates, nitrates, oxalates or halides are preferably used as salts.
- solvents water, methanol, ethanol, iso-propanol, acetonitrile, dioxane, or mixtures thereof, preferably water, can be used.
- the impregnation of the elements in the material Sn0 2 can be carried out by wet impregnation, impregnation at incipient volume or pore volume, without being these limiting examples. Once the impregnated solid is obtained, it is washed, dried and a calcination process is submitted for the activation of the material prior to its use in reaction.
- the catalyst described can be used for the inventive process as it is obtained once calcined.
- the catalyst described above can be supported and / or diluted on a solid such as: silica, alumina, titanium oxide or mixtures thereof, as well as silicon carbide.
- a solid such as: silica, alumina, titanium oxide or mixtures thereof, as well as silicon carbide.
- the fixing of the different catalyst elements on the support can be carried out by conventional impregnation methods, such as pore volume, excess solution, or simply by precipitation on the support of a solution containing the active elements.
- a catalyst can be used that starting from the formula with the composition Sn a Nb b TicM d Oe, in which d is zero, has the following empirical formula:
- - a is between 0.05 and 10.0
- - e has a value that depends on the oxidation state of the elements Sn, Nb and Ti.
- the catalyst must comply with the condition that the catalyst comprises at least Sn, Nb and Ti, and that, in its calcined form, it is presented as a mixed metal oxide formed mostly by the rutile-like crystalline phase of Sn0 2 in which at least Nb and / or Ti are incorporated.
- Said catalyst can be prepared by conventional methods from solutions of compounds of the different elements, solutions of the same pure elements, or mixing thereof, with the desired atomic ratios.
- Said solutions are preferably aqueous solutions.
- the catalyst is obtained by a process comprising at least:
- the mixing step can be carried out from the compounds of the different elements, from the pure elements themselves in solution, using co-precipitation methods or by hydrothermal methods.
- the elements Sn, Nb and Ti can be incorporated into the mixing stage as pure metal elements, as salts, as oxides, as hydroxides, as alkoxides, or as mixtures of two or more of the aforementioned forms.
- As salts, sulfates, nitrates, oxalates or halides are preferably used, without these limiting examples.
- the Sn can be incorporated into the mixing stage preferably as tin oxide, tin acetate, tin nitrate, tin chloride, tin fluoride, tin isopropoxide, tin oxalate or tin sulfate.
- the Nb can be incorporated into the mixing step preferably as niobium pentoxide, niobium oxalate, niobium chloride or Nb metal.
- the Ti can be incorporated into the mixing stage preferably as titanium dioxide, titanium oxychloride, titanium oxy sulfate, titanium nitrate, titanium tetrachloride, titanium ethoxide, titanium isopropoxide, titanium butoxide or Ti metal.
- the mixing step can be followed by a period of static permanence in the reactor, or the mixing can be carried out with stirring. Both static permanence and agitation can be performed in a normal reactor or in an autoclave.
- the mixing step can be carried out in solution or by hydrothermal treatment.
- the drying step can be carried out by conventional methods in an oven, evaporation with stirring, evaporation in a rotary evaporator, or vacuum drying.
- the step of calcining the dry solid can be carried out under an inert gas atmosphere, such as nitrogen, helium, argon or mixtures thereof, as well as air or mixtures of air with other gases.
- an inert gas atmosphere such as nitrogen, helium, argon or mixtures thereof, as well as air or mixtures of air with other gases.
- This calcination stage can be carried out by passing a flow of inert gas (with space velocities between 1 and 400 h 1 ) or in static.
- the temperature is preferably in a range between 250 and 850 ° C and more preferably between 400 and 600 ° C.
- the calcination time is not decisive, but it is preferred that it is in a range between 0.5 hours and 20 hours.
- the heating rate is not decisive, but is preferred in a range between 0.1 ° C / minute and 10 ° C / minute.
- the catalyst may also be initially calcined in an oxidizing atmosphere to a temperature between 200 and 350 ° C, and more preferably between 240 and 290 ° C, and subsequently subjected to a calcination in an inert atmosphere.
- the catalyst is obtained, as indicated above, by co-precipitation of the elements, either from precursor compounds containing the different elements or from the pure elements themselves in solution.
- precursor compounds containing the elements Sn, Nb and Ti
- salts, oxides, hydroxides, alkoxides or mixtures of two or more of the aforementioned forms can be used.
- Sulfates, nitrates, oxalates or halides are preferably used as salts.
- solvents water, methanol, ethanol, iso-propanol, acetonitrile, dioxane, or mixtures thereof, preferably water, can be used.
- Co-precipitation of the elements in the solution is carried out by controlled change of pH by the addition of a basic compound selected from alkali metal hydroxides, alkaline earth metal hydroxides, ammonium hydroxide or ammonia water, and alkali metal hypochlorites, Without being these limiting examples.
- a basic compound selected from alkali metal hydroxides, alkaline earth metal hydroxides, ammonium hydroxide or ammonia water, and alkali metal hypochlorites, Without being these limiting examples.
- the catalyst is obtained using hydrothermal methods (containing two or more elements in the synthesis, especially containing Sn, Nb and Ti) in which the temperature and synthesis time can be decisive.
- the synthesis temperature is preferably between 100 and 250 ° C and, more preferably, between 150 and 180 ° C.
- the synthesis time is preferably between 6 and 500 hours, and more preferably between 24 and 200 hours.
- the catalyst is obtained by impregnating the precursors containing the elements Nb and Ti on a Sn0 2 material, presenting mostly the rutile crystalline phase.
- precursor compounds containing the elements Nb and Ti salts, oxides, hydroxides, alkoxides or mixtures of two or more of the aforementioned forms can be used. Sulfates, nitrates, oxalates or halides are preferably used as salts.
- solvents water, methanol, ethanol, iso-propanol, acetonitrile, dioxane, or mixtures thereof, preferably water, can be used.
- the impregnation of the elements in the Sn0 2 material can be carried out by wet impregnation, impregnation at incipient volume or pore volume, without being these limiting examples.
- the impregnated solid is obtained, it is washed, dried and a calcination process is submitted for the activation of the material prior to its use in reaction.
- the catalyst described can be used for the inventive process as it is obtained once calcined.
- the catalyst described above can be supported and / or diluted on a solid such as: silica, alumina, titanium oxide or mixtures thereof, as well as silicon carbide.
- a solid such as: silica, alumina, titanium oxide or mixtures thereof, as well as silicon carbide.
- the fixing of the different catalyst elements on the support can be carried out by conventional impregnation methods, such as pore volume, excess solution, or simply by precipitation on the support of a solution containing the active elements.
- a catalyst can be used that starting from the formula with the composition Sn a Nb b TicM d Oe, in which c is zero, has the following empirical formula:
- - M is a chemical element of the group of transition metals, rare earths or lanthanides
- - d is between 0 and 4.0
- - e has a value that depends on the oxidation state of the elements Sn, Nb and M.
- the above formula must comply with the condition that the catalyst comprises at least Sn and Nb and that, in its calcined form, it is presented as a mixed metal oxide formed mostly by the rutile-like crystalline phase of Sn0 2 in which the Nb is incorporated into the structure of the rutile phase.
- Said catalyst can be prepared by conventional methods from solutions of compounds of the different elements, solutions of the same pure elements, or mixing thereof, with the desired atomic ratios. Said solutions are preferably aqueous solutions.
- the catalyst described in this embodiment can be obtained by a process comprising at least:
- the mixing step can be carried out from the compounds of the different elements, from the pure elements themselves in solution, using co-precipitation methods or by hydrothermal methods.
- the elements Sn, Nb and the metal M can be incorporated into the mixing stage as pure metal elements, as salts, as oxides, as hydroxides, as alkoxides, or as mixtures of two or more of the aforementioned forms.
- salts sulfates, nitrates, oxalates or halides are preferably used, without these limiting examples.
- the Sn can be incorporated into the mixing stage preferably as tin oxide, tin acetate, tin nitrate, tin chloride, tin fluoride, tin isopropoxide, tin oxalate or tin sulfate.
- the Nb can be incorporated into the mixing step preferably as niobium pentoxide, niobium oxalate, niobium chloride or Nb metal.
- the mixing step can be followed by a period of static permanence in the reactor, or the mixing can be carried out with stirring. Both static permanence and agitation can be performed in a normal reactor or in an autoclave.
- the mixing step can be carried out in solution or by hydrothermal treatment.
- the drying step can be carried out by conventional methods in an oven, evaporation with stirring, evaporation in rotary evaporator, or vacuum drying.
- the step of calcining the dry solid can be carried out under an inert gas atmosphere, such as nitrogen, helium, argon or mixtures thereof, as well as air or mixtures of air with other gases.
- This calcination stage can be carried out by passing a flow of inert gas (with space velocities between 1 and 400 h 1 ) or in static.
- the temperature is preferably in a range between 250 and 850 ° C and more preferably between 400 and 600 ° C.
- the calcination time is not decisive, but it is preferred that it is in a range between 0.5 hours and 20 hours.
- the heating rate is not decisive, but is preferred in a range between 0.1 ° C / minute and 10 ° C / minute.
- the catalyst may also be initially calcined in an oxidizing atmosphere to a temperature between 200 and 350 ° C, and more preferably between 240 and 290 ° C, and subsequently subjected to calcination in an inert atmosphere.
- the catalyst is obtained, as indicated above, by co-precipitation of the elements, either from precursor compounds containing the different elements or from the pure elements themselves in solution.
- precursor compounds containing the elements Sn, Nb and the element M salts, oxides, hydroxides, alkoxides or mixtures of two or more of the aforementioned forms can be used. Sulfates, nitrates, oxalates or halides are preferably used as salts.
- solvents water, methanol, ethanol, iso-propanol, acetonitrile, dioxane, or mixtures thereof, preferably water, can be used.
- Co-precipitation of the elements in the solution is carried out by controlled change of pH by the addition of a basic compound selected from alkali metal hydroxides, alkaline earth metal hydroxides, ammonium hydroxide or ammonia water, and alkali metal hypochlorites, Without being these limiting examples.
- a basic compound selected from alkali metal hydroxides, alkaline earth metal hydroxides, ammonium hydroxide or ammonia water, and alkali metal hypochlorites, Without being these limiting examples.
- the catalyst is obtained using hydrothermal methods (containing two or more elements in the synthesis, especially containing Sn, Nb and element M) in which the temperature and synthesis time can be decisive.
- the synthesis temperature is found, preferably, between 100 and 250 ° C and, more preferably, between 150 and 180 ° C.
- the synthesis time is preferably between 6 and 500 hours, and more preferably between 24 and 200 hours.
- the catalyst is obtained by impregnating the precursors containing Nb and the metal M on a Sn0 2 material, mostly presenting the rutile crystalline phase.
- precursor compounds containing Nb and element M salts, oxides, hydroxides, alkoxides or mixtures of two or more of the aforementioned forms can be used. Sulfates, nitrates, oxalates or halides are preferably used as salts.
- solvents water, methanol, ethanol, iso-propanol, acetonitrile, dioxane, or mixtures thereof, preferably water, can be used.
- the impregnation of the elements in the material Sn0 2 can be carried out by wet impregnation, impregnation at incipient volume or pore volume, without being these limiting examples. Once the impregnated solid is obtained, it is washed, dried and a calcination process is submitted for the activation of the material prior to its use in reaction.
- the catalyst described can be used for the inventive process as it is obtained once calcined.
- the catalyst described above in this invention can be supported and / or diluted on a solid such as: silica, alumina, titanium oxide or mixtures thereof, as well as silicon carbide.
- a solid such as: silica, alumina, titanium oxide or mixtures thereof, as well as silicon carbide.
- the fixing of the different catalyst elements on the support can be carried out by conventional impregnation methods, such as pore volume, excess solution, or simply by precipitation on the support of a solution containing the active elements.
- a catalyst can be used that starting from the formula with the composition Sn a Nb b TicM d Oe, in which c and d are zero, has the following empirical formula:
- - a and b are between 0.05 and 10.0
- the catalyst comprises at least Sn and Nb and that, in its calcined form, it is presented as a mixed metal oxide formed mostly by the rutile-like crystalline phase of Sn0 2 in which Nb is incorporated into the Rutile phase structure.
- Said catalyst can be prepared by conventional methods from solutions of compounds of the different elements, solutions of the same pure elements, or mixing thereof, with the desired atomic ratios.
- Said solutions are preferably aqueous solutions.
- the catalyst is obtained by a process comprising at least:
- the mixing step can be carried out from the compounds of the different elements, from the pure elements themselves in solution, using co-precipitation methods or by hydrothermal methods.
- the elements Sn and Nb can be incorporated into the mixing stage as pure metal elements, as salts, as oxides, as hydroxides, as alkoxides, or as mixtures of two or more of the aforementioned forms.
- salts sulfates, nitrates, oxalates or halides are preferably used, without these limiting examples.
- the Sn can be incorporated into the mixing stage preferably as tin oxide, tin acetate, tin nitrate, tin chloride, tin fluoride, tin isopropoxide, tin oxalate or tin sulfate.
- the Nb can be incorporated into the mixing step preferably as niobium pentoxide, niobium oxalate, niobium chloride or Nb metal.
- the mixing step can be followed by a period of static permanence in the reactor, or the mixing can be carried out with stirring. Both static permanence and agitation can be performed in a normal reactor or in a autoclave.
- the mixing step can be carried out in solution or by hydrothermal treatment.
- the drying step can be carried out by conventional methods in an oven, evaporation with stirring, evaporation in a rotary evaporator, or vacuum drying.
- the step of calcining the dry solid can be carried out under an inert gas atmosphere, such as nitrogen, helium, argon or mixtures thereof, as well as air or mixtures of air with other gases.
- an inert gas atmosphere such as nitrogen, helium, argon or mixtures thereof, as well as air or mixtures of air with other gases.
- This calcination stage can be carried out by passing a flow of inert gas (with space velocities between 1 and 400 h 1 ) or in static.
- the temperature is preferably in a range between 250 and 850 ° C and more preferably between 400 and 600 ° C.
- the calcination time is not decisive, but it is preferred that it is in a range between 0.5 hours and 20 hours.
- the heating rate is not decisive, but is preferred in a range between 0.1 ° C / minute and 10 ° C / minute.
- the catalyst may also be initially calcined in an oxidizing atmosphere to a temperature between 200 and 350 ° C, and more preferably between 240 and 290 ° C, and subsequently subjected to calcination in an inert atmosphere.
- the catalyst is obtained, as indicated above, by co-precipitation of the elements, either from precursor compounds containing the different elements or from the pure elements themselves in solution.
- precursor compounds containing the elements Sn and Nb
- Sulfates, nitrates, oxalates or halides are preferably used as salts.
- solvents water, methanol, ethanol, iso-propanol, acetonitrile, dioxane, or mixtures thereof, preferably water, can be used.
- Co-precipitation of the elements in the solution is carried out by controlled change of pH by the addition of a basic compound selected from alkali metal hydroxides, alkaline earth metal hydroxides, ammonium hydroxide or ammonia water, and alkali metal hypochlorites, Without being these limiting examples.
- a basic compound selected from alkali metal hydroxides, alkaline earth metal hydroxides, ammonium hydroxide or ammonia water, and alkali metal hypochlorites, Without being these limiting examples.
- the catalyst is obtained using hydrothermal methods (containing at least two elements in the synthesis, especially Sn and Nb) in which the temperature and time of synthesis can be decisive.
- the synthesis temperature is preferably between 100 and 250 ° C and, more preferably, between 150 and 180 ° C.
- the synthesis time is preferably between 6 and 500 hours, and more preferably between 24 and 200 hours.
- the catalyst is obtained by impregnating precursors containing Nb on a Sn0 2 material, mostly presenting the rutile crystalline phase.
- precursor compounds containing Nb salts, oxides, hydroxides, alkoxides or mixtures of two or more of the aforementioned forms can be used. Sulfates, nitrates, oxalates or halides are preferably used as salts.
- solvents water, methanol, ethanol, iso-propanol, acetonitrile, dioxane, or mixtures thereof, preferably water, can be used.
- the impregnation of the Nb in the material Sn0 2 can be carried out by wet impregnation, impregnation at incipient volume or pore volume, without being these limiting examples.
- the impregnated solid is obtained, it is washed, dried and a calcination process is submitted for the activation of the material prior to its use in reaction.
- the catalyst described can be used for the inventive process as it is obtained once calcined.
- the catalyst described above in this invention can be supported and / or diluted on a solid such as: silica, alumina, titanium oxide or mixtures thereof, as well as silicon carbide.
- a solid such as: silica, alumina, titanium oxide or mixtures thereof, as well as silicon carbide.
- the fixing of the different catalyst elements on the support can be carried out by conventional impregnation methods, such as pore volume, excess solution, or simply by precipitation on the support of a solution containing the active elements.
- a catalyst can be used that starting from the formula with the composition Sn a Nb b Ti c M d O e , in which b is zero, has the following empirical formula:
- - M is a chemical element of the group of transition metals, rare earths or lanthanides
- - d is between 0 and 4.0
- - e has a value that depends on the oxidation state of the elements Sn, Ti and M.
- the above formula must comply with the condition that the catalyst comprises at least Sn and Ti and that, in its calcined form, it is presented as a mixed metal oxide formed mostly by the rutile-like crystalline phase of Sn0 2 in which the Ti is incorporated into the structure of the rutile phase.
- Said catalyst can be prepared by conventional methods from solutions of compounds of the different elements, solutions of the same pure elements, or mixing thereof, with the desired atomic ratios.
- Said solutions are preferably aqueous solutions.
- the mixing step can be carried out from the compounds of the different elements, from the pure elements themselves in solution, using co-precipitation methods or by hydrothermal methods.
- the elements Sn, Ti and the metal M can be incorporated into the mixing stage as pure metal elements, as salts, as oxides, as hydroxides, as alkoxides, or as mixtures of two or more of the aforementioned forms.
- How salts are used preferably sulfates, nitrates, oxalates or halides, without being these limiting examples.
- the Sn can be incorporated into the mixing stage preferably as tin oxide, tin acetate, tin nitrate, tin chloride, tin fluoride, tin isopropoxide, tin oxalate or tin sulfate.
- the Ti can be incorporated into the mixing stage preferably as titanium dioxide, titanium oxychloride, titanium oxy sulfate, titanium nitrate, titanium tetrachloride, titanium ethoxide, titanium isopropoxide, titanium butoxide or Ti metal.
- the mixing step can be followed by a period of static permanence in the reactor, or the mixing can be carried out with stirring. Both static permanence and agitation can be performed in a normal reactor or in an autoclave.
- the mixing step can be carried out in solution or by hydrothermal treatment.
- the drying step can be carried out by conventional methods in an oven, evaporation with stirring, evaporation in a rotary evaporator, or vacuum drying.
- the step of calcining the dry solid can be carried out under an inert gas atmosphere, such as nitrogen, helium, argon or mixtures thereof, as well as air or mixtures of air with other gases.
- an inert gas atmosphere such as nitrogen, helium, argon or mixtures thereof, as well as air or mixtures of air with other gases.
- This calcination stage can be carried out by passing a flow of inert gas (with space velocities between 1 and 400 h 1 ) or in static.
- the temperature is preferably in a range between 250 and 850 ° C and more preferably between 400 and 600 ° C.
- the calcination time is not decisive, but it is preferred that it is in a range between 0.5 hours and 20 hours.
- the heating rate is not decisive, but is preferred in a range between 0.1 ° C / minute and 10 ° C / minute.
- the catalyst may also be initially calcined in an oxidizing atmosphere to a temperature between 200 and 350 ° C, and more preferably between 240 and 290 ° C, and subsequently subjected to a calcination in an inert atmosphere.
- the catalyst is obtained, as indicated above, by co-precipitation of the elements, either from precursor compounds containing the different elements or from the pure elements themselves in solution.
- precursor compounds containing the elements Sn, Ti and the element M salts, oxides, hydroxides, alkoxides or mixtures of two or more of the aforementioned forms can be used. Sulfates, nitrates, oxalates or halides are preferably used as salts.
- solvents water, methanol, ethanol, iso-propanol, acetonitrile, dioxane, or mixtures thereof, preferably water, can be used.
- Co-precipitation of the elements in the solution is carried out by controlled change of pH by the addition of a basic compound selected from alkali metal hydroxides, alkaline earth metal hydroxides, ammonium hydroxide or ammonia water, and alkali metal hypochlorites, Without being these limiting examples.
- a basic compound selected from alkali metal hydroxides, alkaline earth metal hydroxides, ammonium hydroxide or ammonia water, and alkali metal hypochlorites, Without being these limiting examples.
- the catalyst is obtained using hydrothermal methods (containing two or more elements in the synthesis, especially containing Sn, Ti and element M) in which the temperature and synthesis time can be decisive.
- the synthesis temperature is preferably between 100 and 250 ° C and, more preferably, between 150 and 180 ° C.
- the synthesis time is preferably between 6 and 500 hours, and more preferably between 24 and 200 hours.
- the catalyst is obtained by impregnating the precursors containing Ti and the metal M onto a Sn0 2 material, mostly presenting the rutile crystalline phase.
- precursor compounds containing Ti and element M salts, oxides, hydroxides, alkoxides or mixtures of two or more of the aforementioned forms can be used. Sulfates, nitrates, oxalates or halides are preferably used as salts.
- solvents water, methanol, ethanol, iso-propanol, acetonitrile, dioxane, or mixtures thereof, preferably water, can be used.
- the impregnation of the elements in the Sn0 2 material can be carried out by wet impregnation, impregnation at incipient volume or pore volume, without being these limiting examples.
- the impregnated solid is obtained, it is washed, dried and a calcination process is submitted for the activation of the material prior to its use in reaction.
- the catalyst described can be used for the inventive process as it is obtained once calcined.
- the catalyst described above in this invention can be supported and / or diluted on a solid such as: silica, alumina, titanium oxide or mixtures thereof, as well as silicon carbide.
- a solid such as: silica, alumina, titanium oxide or mixtures thereof, as well as silicon carbide.
- the fixing of the different catalyst elements on the support can be carried out by conventional impregnation methods, such as pore volume, excess solution, or simply by precipitation on the support of a solution containing the active elements.
- a catalyst can be used that starting from the formula with the composition Sn a Nb b Ti c M d O e , in which b and d are zero, has the following empirical formula:
- - e has a value that depends on the oxidation state of the elements Sn and Ti.
- the catalyst comprises at least Sn and Ti and that, in its calcined form, it is presented as a mixed metal oxide formed mostly by the rutile-like crystalline phase of Sn0 2 in which the Ti is incorporated into the structure of the rutile phase
- Said catalyst can be prepared by conventional methods from solutions of compounds of the different elements, from solutions of the same pure elements, or from mixing of both, with the desired atomic ratios.
- Said solutions are preferably aqueous solutions.
- the catalyst can be obtained by a process comprising at least: a) a first stage, of mixing of compounds of the different elements, of pure elements, or of mixing of both,
- the mixing step can be carried out from the compounds of the different elements, from the pure elements themselves in solution, using co-precipitation methods or by hydrothermal methods.
- the elements Sn and Ti can be incorporated into the mixing stage as pure metal elements, as salts, as oxides, as hydroxides, as alkoxides, or as mixtures of two or more of the aforementioned forms.
- salts sulfates, nitrates, oxalates or halides are preferably used, without these limiting examples.
- the Sn can be incorporated into the mixing stage preferably as tin oxide, tin acetate, tin nitrate, tin chloride, tin fluoride, tin isopropoxide, tin oxalate or tin sulfate.
- the Ti can be incorporated into the mixing stage preferably as titanium dioxide, titanium oxychloride, titanium oxy sulfate, titanium nitrate, titanium tetrachloride, titanium ethoxide, titanium isopropoxide, titanium butoxide or Ti metal.
- the mixing step can be followed by a period of static permanence in the reactor, or the mixing can be carried out with stirring. Both static permanence and agitation can be performed in a normal reactor or in an autoclave.
- the mixing step can be carried out in solution or by hydrothermal treatment.
- the drying step can be carried out by conventional methods in an oven, evaporation with stirring, evaporation in a rotary evaporator, or vacuum drying.
- the step of calcining the dry solid can be carried out under an inert gas atmosphere, such as nitrogen, helium, argon or mixtures thereof, as well as of air or mixtures of air with other gases.
- an inert gas atmosphere such as nitrogen, helium, argon or mixtures thereof, as well as of air or mixtures of air with other gases.
- This calcination stage can be carried out by passing a flow of inert gas (with space velocities between 1 and 400 h 1 ) or in static.
- the temperature is preferably in a range between 250 and 850 ° C and more preferably between 400 and 600 ° C.
- the calcination time is not decisive, but it is preferred that it is in a range between 0.5 hours and 20 hours.
- the heating rate is not decisive, but is preferred in a range between 0.1 ° C / minute and 10 ° C / minute.
- the catalyst may also be initially calcined in an oxidizing atmosphere to a temperature between 200 and 350 ° C, and more preferably between 240 and 290 ° C, and subsequently subjected to calcination in an inert atmosphere.
- the catalyst is obtained, as indicated above, by co-precipitation of the elements, either from precursor compounds containing the different elements or from the pure elements themselves in solution.
- precursor compounds containing the elements Sn and Ti
- salts, oxides, hydroxides, alkoxides or mixtures of two or more of the aforementioned forms can be used.
- Sulfates, nitrates, oxalates or halides are preferably used as salts.
- solvents water, methanol, ethanol, iso-propanol, acetonitrile, dioxane, or mixtures thereof, preferably water, can be used.
- Co-precipitation of the elements in the solution is carried out by controlled change of pH by the addition of a basic compound selected from alkali metal hydroxides, alkaline earth metal hydroxides, ammonium hydroxide or ammonia water, and alkali metal hypochlorites, Without being these limiting examples.
- a basic compound selected from alkali metal hydroxides, alkaline earth metal hydroxides, ammonium hydroxide or ammonia water, and alkali metal hypochlorites, Without being these limiting examples.
- the solution is allowed to age and subsequently the solid obtained is washed, dried and a calcination process is submitted for the activation of the material prior to its use in reaction.
- the catalyst is obtained using hydrothermal methods (containing at least two elements in the synthesis, especially Sn and Ti) in which the temperature and synthesis time can be decisive.
- the synthesis temperature is preferably between 100 and 250 ° C and, more preferably, between 150 and 180 ° C.
- the synthesis time is preferably
- the catalyst is obtained by impregnating Ti precursors onto a Sn0 2 material, mostly presenting the rutile crystalline phase.
- precursor compounds containing Ti e they can use salts, oxides, hydroxides, alkoxides or mixtures of two or more of the aforementioned forms. Sulfates, nitrates, oxalates or halides are preferably used as salts.
- solvents water, methanol, ethanol, iso-propanol, acetonitrile, dioxane, or mixtures thereof, preferably water, can be used.
- the impregnation of the elements in the material Sn0 2 can be carried out by wet impregnation, impregnation at incipient volume or pore volume, without being these limiting examples.
- the impregnated solid is obtained, it is washed, dried and a calcination process is submitted for the activation of the material prior to its use in reaction.
- the catalyst described according to this embodiment can be used for the inventive process as it is obtained once calcined.
- the catalyst described above in this invention can be supported and / or diluted on a solid such as: silica, alumina, titanium oxide or mixtures thereof, as well as silicon carbide.
- a solid such as: silica, alumina, titanium oxide or mixtures thereof, as well as silicon carbide.
- the fixing of the different catalyst elements on the support can be carried out by conventional impregnation methods, such as pore volume, excess solution, or simply by precipitation on the support of a solution containing the active elements.
- - catalysts comprising Sn and Nb, Sn and Ti, and combinations of Sn-Nb or Sn-Ti with other elements, in which at least Sn and Nb or Sn and Ti are present in the form of a mixed oxide, provide yields to C5-C8 hydrocarbons greater than those reported with Ce-Zr-based catalysts, with total yields (“20%) comparable to those observed for these Ce-Zr materials; - they are more stable and resistant in reaction conditions than other materials reported catalysts;
- the metal M may be selected from the group of transition metals, preferably V, Cr, Fe, Co, Ni, Cu, Zn, Mo, Ta, TI, Re and combinations thereof; as well as rare earths and lanthanides, preferably La.
- the metal M is selected from among V, Mn, Cu, Zn, La and combinations thereof.
- the product obtained can be selected from linear, branched, cyclic aliphatic hydrocarbons of between 5 and 16 C atoms, and may also contain between 0 and 4 O atoms, and more preferably between 0 and 2 atoms from O.
- the product obtained may be selected from among aromatic compounds of between 5 and 16 C atoms, and may also contain between 0 and 4 O atoms.
- the aqueous mixture derived from the Biomass that is introduced in the first step may contain oxygenated organic compounds that have between 1 and 12 carbon atoms, preferably between 1 and 9 carbon atoms, and also may have between 1 and 9 oxygen atoms, preferably of between 1 and 6 oxygen atoms.
- the total concentration of the oxygenated organic compounds present in the aqueous mixture derived from the biomass are preferably in a range of between 0.5 and 99.5% by weight, and more preferably between 1.0 and 70.0% by weight.
- the contact between the aqueous mixture and the catalyst is carried out in a reactor preferably selected from a discontinuous reactor, a continuous stirred tank reactor, a continuous fixed bed reactor and a continuous reactor of fluidized bed
- the reactor is a discontinuous reactor and the reaction is carried out in a liquid phase at a pressure preferably selected from 1 to 80 bars, and more preferably at a pressure between 1 and 50 bars.
- the reaction can be carried out at a temperature between 100 ° C and 350 ° C, preferably between 140 ° C and 280 ° C.
- the contact time between the aqueous mixture containing the oxygenated organic compounds derived from the biomass and the catalyst may range from 2 minutes to 200 hours, preferably from 1 hour to 100 hours.
- the weight ratio between the aqueous mixture containing the oxygenated compounds derived from the biomass and the catalyst can be preferably between 1 and 200, and more preferably between 2.5 and 100.
- the reactor that is used in the process of the present invention can be a fixed bed reactor or a fluidized bed reactor.
- the reaction temperature is preferably in a range between 100 ° C and 350 ° C and more preferably between 150 ° C and 300 ° C;
- the contact time (W / F) is between 0.001 and 200 s; and the working pressure of between 1 and 100 bars and more preferably between 1 and 60 bars.
- the contact between the aqueous fraction containing the oxygenated organic compounds and the catalyst can be carried out under nitrogen, argon, air atmosphere, nitrogen enriched air, argon enriched air, or combinations of the same.
- the process is preferably carried out in a nitrogen atmosphere.
- the process is preferably carried out in an atmosphere of air or air enriched with nitrogen.
- the present invention describes the use of the catalyst obtained as described above to obtain mixtures of hydrocarbons and aromatic compounds, preferably between 5 and 16 C (C5-C16) atoms useful in liquid fuels, a from the catalytic transformation of oxygenated organic compounds present in aqueous fractions derived from biomass.
- the aqueous fractions derived from the biomass containing different oxygenated organic compounds to be treated by the process of the present invention may be selected from among aqueous fractions obtained by liquid-liquid separation of the bio-liquids produced by thermal pyrolysis and / or catalytic biomass , aqueous fractions obtained by chemical and / or enzymatic biomass hydrolysis, aqueous fractions obtained by liquefaction under sub- or super-critical biomass conditions, and aqueous fractions obtained from biomass fermentation for the selective production of ethanol, butanol, succinic acid , and lactic acid, without being these limiting examples.
- the aqueous fractions derived from the biomass to be treated by the process of the present invention may contain different oxygenated organic compounds having between 1 and 12 Carbon atoms, preferably between 1 and 9 Carbon atoms.
- aqueous fractions derived from the biomass to be treated by the process of the present invention may contain different oxygenated organic compounds possessing between 1 and 9 Oxygen atoms, preferably between 1 and 6 O atoms.
- the aqueous fractions derived from the biomass to be treated by the process of the present invention may contain different oxygenated organic compounds in concentrations ranging between 0.5 and 99.5% by weight with respect to the amount of water, preferably of between 1.0 and 70.0% by weight with respect to the amount of water.
- the aqueous fractions derived from the biomass to be treated by the process of the present invention may contain different oxygenated organic compounds, including alcohols, aldehydes, ketones, acids and carboxylic di-acids, asters, ethers, diols, triols and polyols in general, sugars, fury derivatives, and phenolic derivatives, without being these limiting examples.
- oxygenated organic compounds including alcohols, aldehydes, ketones, acids and carboxylic di-acids, asters, ethers, diols, triols and polyols in general, sugars, fury derivatives, and phenolic derivatives, without being these limiting examples.
- the aqueous fractions derived from the biomass to be treated by the process of the present invention may contain different oxygenated organic compounds of the alcohol type, including methanol, ethanol, 1- propanol, 2-propanol, 1-butanol, 2-butanol, 1-pentanol, 2-pentanol, iso-pentanol, 1- hexanol, 2-hexanol, 3-hexanol, and furfuryl alcohol, without being these limiting examples.
- the aqueous fractions derived from the biomass to be treated by the process of the present invention may contain different oxygenated compounds of the aldehyde type, including formaldehyde, acetaldehyde, propanal, butanal, 2-butenal, pentanal, 2-pentenal , 3-pentenal, hexanal, 2-hexenal, 3- hexenal, 2-methyl-2-pentenal, 2-methyl-3-pentenal, 3-methyl-2-pentenal, furfural, and 5-hydroxymethyl-furfural, Without being these limiting examples.
- different oxygenated compounds of the aldehyde type including formaldehyde, acetaldehyde, propanal, butanal, 2-butenal, pentanal, 2-pentenal , 3-pentenal, hexanal, 2-hexenal, 3- hexenal, 2-methyl-2-pentenal, 2-methyl-3-pentenal, 3-methyl-2-pentenal, furfural, and 5-hydroxymethyl-
- the aqueous fractions derived from the biomass to be treated by the process of the present invention may contain different oxygenated organic compounds of the ketone type, including acetone, 2-butanone, 2-pentanone, penten-2-one, 3-pentanone, penten-3-one, 2-hexanone, hexen-2-one, 3- hexanone, hexen-3-one, iso-forone, vanillin, aceto-vanillin, syringone, and aceto-syringone, without being these limiting examples.
- the aqueous fractions derived from the biomass to be treated by the process of the present invention may contain different oxygenated organic compounds of the acid and di-acid type, including acetic acid, propionic acid, butyric acid, pentanoic acid, hexanoic acid, lactic acid, pyruvic acid, levulinic acid, tartronic acid, tartaric acid, glycolic acid, succinic acid, gluconic acid, and glucaric acid, without being these limiting examples.
- the aqueous fractions derived from the biomass to be treated by the process of the present invention may contain different oxygenated organic compounds of the ester type, including methyl acetate, ethyl acetate, propyl acetate, butyl acetate, methyl propionate, ethyl propionate, propyl propionate, butyl propionate, methyl butyrate, ethyl butyrate, propyl butyrate, and butyl butyrate, without being these limiting examples.
- the aqueous fractions derived from the biomass to be treated by the process of the present invention may contain different oxygenated organic compounds of the ether type, including di-methyl ether, di-ethyl ether, di-propyl ether, di -iso-propyl ether, di-butyl ether, di-sec-butyl ether, methyl-ethyl ether, methyl-propyl ether, methyl-iso-propyl ether, methyl-butyl ether, methyl-sec-butyl ether, ethyl-propyl ether, ethyl-iso-propyl ether, ethyl-butyl ether, ethyl-sec-butyl ether, propyl-butyl ether, and propyl-sec-butyl ether, without being these limiting examples.
- the aqueous fractions derived from the biomass to be treated by the process of the present invention may contain different oxygenated organic compounds of the diols type, including ethylene glycol, 1, 2- propanediol, 1,3-propanediol, 1, 2-butanediol, 1,3-butanediol, 1,4-butanediol, 2,3-butanediol, 1, 2-pentanediol, 1,3-pentanediol, 1,4-pentanediol, 1,5-pentanediol, 2,3- pentanediol, 2,4-pentanediol, 1,2-hexanediol, 1,3-hexanediol, 1,4-hexanediol, 1, 6-hexanediol, 2,3-hexane-diol, 2,4-hexanediol; triols
- the aqueous fractions derived from the biomass to be treated by the process of the present invention may contain different oxygenated organic compounds of the Furyne derivatives type, including furan, 2- methyl furan, 5-methyl furan, 2 , 5-dimethyl-furan, 2-ethyl-furan, 5-ethyl-furan, 2,5-diethyl-furan, benzofuran, methyl benzofuran, ethyl benzofuran, without being these limiting examples.
- Furyne derivatives type including furan, 2- methyl furan, 5-methyl furan, 2 , 5-dimethyl-furan, 2-ethyl-furan, 5-ethyl-furan, 2,5-diethyl-furan, benzofuran, methyl benzofuran, ethyl benzofuran, without being these limiting examples.
- the aqueous fractions derived from biomass to be treated by the process of the present invention may contain different oxygenated compounds of the phenolic derivatives type, including phenol, benzyl alcohol, acetol, o-cresol, m-cresol, p-cresol, guaiacol, vanillin alcohol, siringol, and aceto-siringol, without being these limiting examples.
- the mixtures of organic compounds of between 5 and 16 C atoms (C5-C16) obtained as a result of the transformation of the oxygenated compounds present in aqueous fractions derived from biomass may contain linear, branched, cyclic linear aliphatic hydrocarbon compounds of 5 and 16 C atoms, and may also contain between 0 and 4 O atoms, preferably between 0 and 2 O atoms.
- Mixtures of organic compounds of between 5 and 16 C atoms (C5-C16) obtained as a result of the transformation of oxygenated compounds present in aqueous fractions derived from biomass may contain aromatic compounds of between 5 and 16 C atoms , may also contain between 0 and 4 O atoms, preferably between 0 and 2 O atoms. These aromatic compounds may possess one, two, or more substituents in the ring, these substituents being able to be of the linear, branched and branched alkyl type / or cyclic, linear, branched and / or cyclic alkoxide, acetyl, uranic, furyl, and aromatic tetrahydrof, without being these limiting examples.
- Fig. 1 Shows X-ray diffractograms of catalysts based on Sn [Sn0 2 ], Nb [Nb 2 0 5 ] and Ti [Ti0 2 -Anatase] and [Ti0 2 -Rutile] oxides.
- Fig. 2 Shows X-ray diffractograms of catalysts based on Sn oxides (a) [Sn0 2 ], Nb (b) [Nb 2 0 5 ] and Ti (c) [Ti0 2 ] prepared by co-precipitation described in examples 1, 2 and 3, respectively.
- Fig. 3 Shows X-ray diffractograms of catalysts based on tin and niobium oxides [Sn-Nb-O] described in Examples 4 to 7.
- Fig. 4. Shows X-ray diffractograms of catalysts based on tin and titanium oxides [Sn-Ti-O] described in Examples 8 to 11.
- Fig. 5 Shows X-ray diffractograms of catalysts based on tin oxides, titanium and niobium [Sn-Nb-Ti-O] described in Examples 12 to 15.
- Fig. 6. Shows the X-ray diffractogram of a catalyst based on Ce-Zr-0 (Example 16).
- Fig. 7 Shows X-ray diffractograms of Nb and Ti-based catalysts supported by impregnation over tin oxide [Nb / Sn0 2 and Ti / Sn0 2 ] described in Examples 17 and 18, respectively.
- Fig. 8. It shows a scheme with the chemical structures of reagents and main reaction products, together with the reactions that take place during the process.
- Fig. 9 Shows a comparison of the stability and maintenance of the catalytic activity with the re-uses of the catalysts Sn-Nb-0 (Example 5), Sn-Ti-0 (Example 10) and Ce-Zr-0 (Example 16).
- Example 1 Preparation of a catalyst by co-precipitation method based on tin oxide [Sn0 2 ]
- tin oxide [Sn0 2 ]
- tin oxide (IV) pentahydrate chloride 14.72 g of tin (IV) pentahydrate chloride are added, which are kept under stirring until completely dissolved.
- the resulting gel is transferred to a container where it is allowed to age for 24 hours at room temperature.
- the solid After a washing and filtering step, the solid is dried at 100 ° C overnight.
- the solid obtained is heated at 600 ° C for 2 h in a stream of air to obtain the catalyst.
- This catalyst is characterized by presenting an X-ray diffractogram as shown in Figure 2a.
- Example 2 Preparation of a catalyst by co-precipitation method, based on niobium oxide [Nb 2 0 5 ]
- Example 3 Preparation of a catalyst by co-precipitation method, based on titanium oxide [Ti0 2 ]
- This catalyst was synthesized to illustrate catalysts of the type Ce-Zr mixed oxides commonly used in literature for this type of condensation reactions [A. Gangadharan et al., Appl. Tasting! A: Gral., 385 (2010) 80] Various catalysts with different Ce-Zr ratios were synthesized, and the catalyst that provided the best results, in terms of yield to organic and conversion was selected to be compared with the catalysts herein. invention.
- the catalyst was prepared by the synthesis method by co-precipitation of the mixed oxide Ce-Zr adapting the procedure published by Serrano-Ruiz et al. [J. Caial., 241 (2006) 45-55]
- an aqueous solution of the salts of both metals in equimolar proportion is prepared.
- 150 ml of water are added 11, 76 g of Ce (N0 3 ) 3 -6H 2 0 and 6.70 g of Zr0 (N0 3 ) 2 H 2 0, which are kept under stirring until completely dissolved.
- the solution is transferred to a balloon where it is allowed to age under stirring and at room temperature for 65 h. After a washing and filtering step, the solid is dried at 100 ° C overnight. Finally, the solid obtained is heated at 450 ° C for 2 h in a stream of air to obtain the catalyst.
- the amounts of Ce and Zr measured by ICP coincide with the formula Ce 0, Zr 0, O 2 , and the X-ray diffractogram obtained for this sample indicates the presence of mixed oxides of Ce and Zr (Fig. 6)
- Example 17 Preparation of a catalyst based on mixed tin and niobium oxides [Nb-Sn0 2 impregnated] using an impregnation method
- a mixed oxide type catalyst with an Sn-Nb ratio similar to that used for the catalyst of Example 4 was synthesized, in order to be compared in terms of catalytic activity with the catalysts of the present invention.
- the catalyst was prepared by the pore volume impregnation synthesis method.
- Nb-SN0 2 an aqueous solution containing 1 86g of niobium oxalate in a volume of water precalculated to impregnate about 1, 5 g of commercial SN0 2 is prepared.
- the solution is added drop by drop on said support until a homogeneous gel is obtained.
- the solid obtained is heated at 600 ° C for 2 h in a stream of air to obtain the catalyst.
- This catalyst is characterized by presenting an X-ray diffractogram as shown in Figure 7a.
- Example 18 Preparation of a catalyst based on mixed oxides of Sn and Ti [Ti-Sn0 2 impregnated] using an impregnation method
- a mixed oxide type catalyst was synthesized with an Sn-Ti ratio similar to that used for the catalyst of Example 8, in order to be compared in terms of catalytic activity with the catalysts of the present invention.
- the catalyst was prepared by the pore volume impregnation synthesis method.
- an aqueous solution containing 0.7 ml of an aqueous solution of titanium oxychloride with hydrochloric acid is prepared in a volume of water previously calculated to impregnate about 1.5 g of commercial Sn0 2 .
- the solution is added dropwise onto said support until a homogeneous gel is obtained.
- the solid obtained is heated at 600 ° C for 2 h in a stream of air to obtain the catalyst.
- This catalyst is characterized by presenting an X-ray diffractogram as shown in Figure 7b.
- Example 19 Comparative catalytic activity of the catalysts of the Sn-Nb series of Examples 1, 2, 4, 5, 6 and 7.
- the catalytic activity experiments were carried out in the liquid phase using 12 ml stainless steel autoclave type reactors with a reinforced PEEK (polyether-ethyl ketone) reinforced interior and equipped with magnetic stirrer, pressure gauge and inlet valve / output of gases and liquid samples.
- the reactors are located on an individual steel jacket support with closed loop temperature control.
- the initial feed consists of a model aqueous mixture containing oxygenated compounds simulating the residual aqueous currents that are obtained after a phase separation process, after the biomass pyrolysis.
- the composition of the model aqueous mixture is detailed below (Table 1):
- Table 1 Composition of the model aqueous mixture used as initial feed in the autoclave type reactor.
- the quantification of the products is carried out from the response factors calculated by internal standard (2% by weight solution of chlorobenzene in methanol) and organic compounds obtained from more than 5 carbon atoms are classified and quantified in ranges or intervals of compounds, whose response factors have been calculated from representative molecules thereof.
- organic compounds obtained from more than 5 carbon atoms are classified and quantified in ranges or intervals of compounds, whose response factors have been calculated from representative molecules thereof.
- main primary condensation reaction products such as acetone, ethyl acetate, 3-pentanone and 2-methyl-2-pentenal
- groups of molecules with 5, 6, 7, 8, 9, 10 or more are distinguished of 10 carbon atoms, produced by consecutive condensation reactions of reagents and primary products.
- these molecules are grouped into two large groups of compounds, namely: Products C5-C8 and Products C9-C10 +.
- the Total Organic Yield (in percentage by weight), was calculated from the following formula:
- Acetic acid can be transformed into ethyl acetate (esterification product) and acetone (ketone product).
- the final products are compounds of type C9 (there are no intermediate or longer chain products in the final mixture).
- Example 20 Comparative catalytic activity of the Sn-Ti series catalysts of Examples 1, 3, 8, 9, 10 and 11.
- Example 21 Comparative catalytic activity of the Sn-Ti-Nb series catalysts of Examples 1, 2, 12, 13, 14 and 15.
- Acetone acetic acid condensation product
- Acetone is present in the final mixture in amounts less than 1.5%, because most of the acetic acid reacts by esterification to produce ethyl acetate.
- acetone is a very reactive compound that can lead to condensation products of higher molecular weight.
- Example 22 Comparative catalytic activity of the Sn-Nb series catalysts (Examples 4 and 5) against Nb-Sn0 2 oxide prepared by impregnation (Example 17) and commercial Nb 2 0 5 (Sigma-Aldrich, CAS 1313 -96-8)
- the conversion of propionaldehyde is the biggest difference between one type of catalyst and others. While catalysts based on combined Sn-Nb structures show conversions> 90%, the commercial niobium catalyst and the Nb-Sn0 2 catalyst (Example 17) have much lower conversions (67-70%). This causes the decrease in the formation of first condensation products such as 2-methyl-2-pentenal and some C5-C8 products, as well as products of greater molecular weight originated by second condensation reactions. In these cases, the Total Organic Yield decreases to 49-56%, which means that the use of catalysts based on specific Sn-Nb structures such as Examples 4 and 5 increases the products by 15-25% obtained in the final reaction mixture of the condensation of oxygenated compounds present in aqueous mixtures derived from biomass. These products are potentially usable as additives in gasoline and refining fractions in general.
- Example 23 Comparative catalytic activity of the Sn-Ti series catalysts (Examples 10 and 11) against Ti-Sn0 2 oxide prepared by impregnation (Example 18) and samples of commercial anatase Ti0 2 (Sigma-Aldrich, CAS 1317-70- 0) and Ti0 2 commercial rutile (Sigma-Aldrich, CAS 1317-80-2)
- the Total Organic Yield decreases to 48-51%, which means that the use of catalysts based on specific Sn-Ti structures such as that of Examples 10 and 11 increases the products obtained by «20% in the final reaction mixture of the condensation of oxygenated compounds present in aqueous mixtures derived from biomass. These products are potentially usable as additives in gasoline and refining fractions in general.
- Example 24 Comparative catalytic activity of the Sn-Nb-O, Sn-Ti-0 and Sn-Ti-Nb-0 series catalysts prepared by co-precipitation method (Examples 4, 5, 10, 11, 12 and 13)
- the yield to 2-methyl-2-pentenal, C9-C10 products and in general yield to Total Organic products can be increased by synthesizing the materials in the appropriate compositions, thus achieving catalysts based on specific Sn-Nb-O structures. , Sn-Ti-0 and Sn-Ti-Nb-0 as in Examples 4, 5, 10, 11, 12 and 13. Example 25.
- Comparative catalytic activity of the Sn-Nb-O, Sn-Ti-0 and Sn-Ti-Nb-O series catalysts prepared by co-precipitation (Examples 5, 10 and 13) against a catalyst of conventional Ce-Zr (Example 16) 3000 mg of the model aqueous mixture and 150 mg of one of the catalytic materials of Examples 5, 10, 13 and 16 were introduced into the autoclave reactor described above.
- the reactor was sealed tightly, initially pressurized with 13 bars of N 2 , and heated to 200 ° C under continuous stirring. Liquid samples ( ⁇ 50-100 ml) were taken at different time intervals up to 7 hours of reaction.
- the samples were filtered and diluted in a standard solution of 2% by weight of chlorobenzene in methanol, and analyzed by gas chromatography on a GC-Bruker 430 equipped with an FID detector and a TRB-624 capillary column.
- 60 m Products are identified by an Agilent 6890 N gas chromatograph coupled with an Agilent 5973 N mass detector (GC-MS) and equipped with an HP-5 MS capillary column 30 m long.
- Example 16 the mixed oxide of Ce-Zr (Ex. 16) is that the first three have higher production of organic compounds in the C5-C8 range, while the mixed oxide prepared in Example 16 is able to more easily catalyze second condensation reactions, increasing the amount of compounds in the C9-C10 + range.
- catalysts based on structures that combine Sn, Nb and / or Ti have results similar to those demonstrated by a catalyst such as Ce 0, Zr 0, O 2 traditionally used in literature for reactions of this type.
- the catalysts of Examples 5, 10, 13 and 16 once used are recovered after the reaction, subjected to a methanol wash and dried at 100 ° C overnight. Subsequently, they are characterized by Elemental Analysis (AE) and Thermogravimetry (TG).
- AE Elemental Analysis
- TG Thermogravimetry
- the AE study shows that the Ce-Zr type catalyst of Example 16 has 3.5% by weight of carbon (organic products deposited in the catalyst) after washing.
- the Sn-Nb-based catalyst of Example 5 only has 0.5% by weight of carbon, demonstrating that a lower deposition of carbonaceous substances occurs during the reactive process, and is therefore less sensitive to deactivation caused by the coke deposition
- the Ce-Zr catalyst of Example 16 has a mass loss of 11.5% at a temperature close to 300 ° C corresponding to the desorption of the absorbed organic products.
- the catalyst of Example 5 only shows a mass loss of 1.5% at said temperature.
- This catalyst also has a mass loss of 1.8% at a temperature close to 100 ° C corresponding to the absorbed water. This amount of absorbed water is also observed in the analysis of TG of the catalyst before being used, so that the presence of water in the reaction medium does not cause damage to the activity of the catalyst or its stability.
- Example 26 Comparative catalytic activity during reuse of the catalysts Sn-Nb-0 (Ex. 5), Sn-Ti-0 (Ex. 10), and Ce-Zr-0 (Ex. 16)
- the Total Organic Yield is decreasing slightly with the number of re-uses in said catalysts, but the drop is more pronounced in the case of the Ce-Zr-0 catalyst of Example 16 with a percentage loss of catalytic activity with respect to the initial 16%, while the Sn-Nb-0 catalyst prepared in Example 5 exhibits excellent stability with a percentage drop in catalytic activity of only 1% (see Figure 8). This means that the activity of the Sn-Nb-0 catalyst prepared in Example 5 remains practically constant after at least 3 consecutive reuses.
- the catalyst based on Sn-Ti-0 of Example 10 exhibits a fall in intermediate catalytic activity (10%) between the Ce-Zr-0 material (Ex.
- the analyzes performed by AE and TG confirm the greater stability of the Sn-Nb-based catalyst of Example 5 and the Sn-Ti-based catalyst of Example 10 compared to the mixed Ce-Zr oxide prepared in Example 16.
- the Sn-Nb material Example. 5
- only 0.5% by weight of carbon is determined by AE after the third reuse (R3); 2.8% in the case of Sn-Ti (Ex. 10)
- the amount of carbon detected in the Ce-Zr catalyst (Ex. 16) after the same number of re-uses reached 4.8 % in weigh Likewise, it is observed by TG analysis that the Sn-Nb catalyst (Ex.
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Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4448898A (en) * | 1982-06-07 | 1984-05-15 | Altantic Richfield Company | Method for producing a vanadium-titanium-tin catalyst exhibiting improved intrinsic surface area |
KR20060095075A (ko) * | 2005-02-25 | 2006-08-30 | 오성화학공업주식회사 | 다가 알코올/지방산 에스테르화 불균일계 촉매 및 이의 적용방법 |
US20130079566A1 (en) | 2011-09-27 | 2013-03-28 | Nevada, | Catalytic process for conversion of biomass into hydrocarbon fuels |
US20140288338A1 (en) | 2010-09-14 | 2014-09-25 | IFP Energies Nouvelles | Methods of upgrading biooil to transportation grade hydrocarbon fuels |
WO2015008110A1 (en) | 2013-07-17 | 2015-01-22 | Selle Royal S.P.A. | Device and method for the manufacturing of a support for the human body |
CN105664914A (zh) * | 2016-01-27 | 2016-06-15 | 安徽大学 | 一种二氧化钛/二氧化锡复合光催化剂材料的制备方法 |
WO2017162900A1 (es) | 2016-03-22 | 2017-09-28 | Consejo Superior De Investigaciones Cientificas (Csic) | Procedimiento para la valorización de compuestos oxigenados presentes en fracciones acuosas derivadas de biomasa |
Family Cites Families (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
AU2008222628B2 (en) | 2007-03-08 | 2013-05-23 | Virent, Inc. | Synthesis of liquid fuels and chemicals from oxygenated hydrocarbons |
US8075642B2 (en) | 2008-04-14 | 2011-12-13 | Wisconsin Alumni Research Foundation | Single-reactor process for producing liquid-phase organic compounds from biomass |
EP2331486A2 (en) * | 2008-08-27 | 2011-06-15 | Virent Energy Systems Inc. | Synthesis of liquid fuels from biomass |
JP5812987B2 (ja) * | 2009-05-20 | 2015-11-17 | 田中貴金属工業株式会社 | リーンバーンエンジン用触媒 |
WO2014167524A1 (en) | 2013-04-11 | 2014-10-16 | Basf Corporation | Titanium stannate silicate, method of preparation and use thereof |
WO2015100268A1 (en) | 2013-12-23 | 2015-07-02 | The Regents Of The University Of California | Mesenchymal stem cells for targeted cancer therapy |
ES2762517T3 (es) * | 2014-03-26 | 2020-05-25 | Neste Oyj | Método para la conversión catalítica de cetoácidos e hidrotratamiento en hidrocarburos |
US11034713B2 (en) * | 2014-06-19 | 2021-06-15 | Haldor Topsoe A/S | Crystalline microporous material mediated conversion of C1-3 oxygenate compounds to C4 oxygenate compounds |
CN105661914A (zh) | 2015-11-27 | 2016-06-15 | 林永勤 | 一种从桌面板侧边出风的餐桌 |
US10167430B2 (en) | 2016-06-28 | 2019-01-01 | Battelle Memorial Institute | Catalytic hydrothermal liquefaction for bio-oil production |
JP6579274B2 (ja) | 2016-08-29 | 2019-09-25 | 信越化学工業株式会社 | 光触媒積層体 |
-
2018
- 2018-05-25 ES ES201830508A patent/ES2732747B2/es active Active
-
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- 2019-05-23 EP EP19806718.3A patent/EP3804848A4/en active Pending
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- 2019-05-23 US US17/058,395 patent/US11839867B2/en active Active
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Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4448898A (en) * | 1982-06-07 | 1984-05-15 | Altantic Richfield Company | Method for producing a vanadium-titanium-tin catalyst exhibiting improved intrinsic surface area |
KR20060095075A (ko) * | 2005-02-25 | 2006-08-30 | 오성화학공업주식회사 | 다가 알코올/지방산 에스테르화 불균일계 촉매 및 이의 적용방법 |
US20140288338A1 (en) | 2010-09-14 | 2014-09-25 | IFP Energies Nouvelles | Methods of upgrading biooil to transportation grade hydrocarbon fuels |
US20130079566A1 (en) | 2011-09-27 | 2013-03-28 | Nevada, | Catalytic process for conversion of biomass into hydrocarbon fuels |
WO2015008110A1 (en) | 2013-07-17 | 2015-01-22 | Selle Royal S.P.A. | Device and method for the manufacturing of a support for the human body |
CN105664914A (zh) * | 2016-01-27 | 2016-06-15 | 安徽大学 | 一种二氧化钛/二氧化锡复合光催化剂材料的制备方法 |
WO2017162900A1 (es) | 2016-03-22 | 2017-09-28 | Consejo Superior De Investigaciones Cientificas (Csic) | Procedimiento para la valorización de compuestos oxigenados presentes en fracciones acuosas derivadas de biomasa |
Non-Patent Citations (17)
Title |
---|
A. CORMAS. IBORRAA. VELTY, CHEMICAL REVIEWS, 2007, pages 2411 |
A. FERNANDEZ-ARROYO ET AL., CATALYSIS SCIENCE & TECHNOLOGY, vol. 7, 2017, pages 5495 - 5499 |
A. GANGADHARAN ET AL., APPL. CATAL. A: GRAL., vol. 385, 2010, pages 80 |
A. GANGADHARAN ET AL., APPLIED CATALYSIS A: GEN, vol. 385, 2010, pages 80 - 91 |
ARCOZZI E ET AL.: "The control of catalytic performance of rutile-type Sn/V/Nb/Sb mixed oxides, catalysts for propane ammoxidation to acrylonitrile", CATALYSIS TODAY, vol. 138, no. 1-2, 15 October 2008 (2008-10-15), pages 97 - 131, XP024098419, DOI: 10.1016/j.cattod.2008.04.044 * |
C.A. GAERTNER ET AL., JOURNAL OF CATALYSIS, vol. 266, 2009, pages 71 |
E. E. LOJOIU ET AL., APPLIED CATALYSIS A: GEN., vol. 323, 2007, pages 147 |
F. CHERUBINI ET AL., BIOFUELS, BIOPRODUCTS AND BIOREFINING, vol. 3, 2009, pages 534 |
FORNELL J ET AL.: "Anodic formation of self-organized Ti(Nb,Sn) oxide nanotube arrays with tuneable aspect ratio and size distribution", ELECTROCHEMISTRY COMMUNICATIONS, vol. 33, 1 May 2013 (2013-05-01), pages 84 - 87, XP028679726, DOI: 10.1016/j.elecom.2013.04.023 * |
G.W. HUBERS. IBORRAA. CORMA, CHEMICAL REVIEWS, vol. 106, 2006, pages 4044 |
GONZALEZ-BORJA M A ET AL.: "Anisole and guaiacol hydrodeoxygenation over monolithic Pt-Sn catalysts", ENERGY AND FUELS, vol. 25, no. 9, 26 July 2011 (2011-07-26), pages 4155 - 4162, XP055655044 * |
KAY LUP ANDREW NG ET. AL.: "A review on reactivity and stability of heterogeneous metal catalysts for deoxygenation of bio-oil model compounds. Introduction, Metal catalysts in deoxygenation process: Sn-based catalyst.", JOURNAL OF INDUSTRIAL AND ENGINEERING CHEMISTRY, vol. 56, 4 July 2017 (2017-07-04), pages 1 - 34, XP085213867 * |
M. ASADIERAGHI ET AL., RENEWABLE AND SUSTAINABLE ENERGY REVIEWS, vol. 36, 2014, pages 286 |
QIANG LU ET AL.: "Catalytic upgrading of biomass fast pyrolysis vapors with titania and zirconia/titania based catalysts", FUEL, vol. 89, no. 8, 1 August 2010 (2010-08-01), pages 2096 - 2103, XP055127573, DOI: 10.1016/j.fuel.2010.02.030 * |
SERRANO-RUIZ ET AL., J. CATAL., vol. 241, 2006, pages 45 - 55 |
VESES A ET AL.: "Catalytic upgrading of biomass derived pyrolysis vapors over metal-loaded ZSM-5 zeolites: Effect of different metal cations on the bio-oil final properties", MICROPOROUS AND MESOPOROUS MATERIALS, vol. 209, 26 January 2015 (2015-01-26), pages 189 - 196, XP029147230, DOI: 10.1016/j.micromeso.2015.01.012 * |
WANG C T ET AL.: "Surface and catalytic properties of doped tin oxide nanoparticles", APPLIED SURFACE SCIENCE, vol. 257, no. 1, 15 October 2010 (2010-10-15), pages 127 - 131, XP027196205 * |
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