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WO2013015996A2 - Obtention de polyols à partir d'une charge de départ contenant des saccharides - Google Patents

Obtention de polyols à partir d'une charge de départ contenant des saccharides Download PDF

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Publication number
WO2013015996A2
WO2013015996A2 PCT/US2012/046342 US2012046342W WO2013015996A2 WO 2013015996 A2 WO2013015996 A2 WO 2013015996A2 US 2012046342 W US2012046342 W US 2012046342W WO 2013015996 A2 WO2013015996 A2 WO 2013015996A2
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WIPO (PCT)
Prior art keywords
feedstock
catalyst
saccharide
group
component
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Ceased
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PCT/US2012/046342
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WO2013015996A3 (fr
Inventor
John Q. Chen
Tom N. Kalnes
Joseph A. Kocal
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Honeywell UOP LLC
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UOP LLC
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Filing date
Publication date
Priority claimed from US13/193,072 external-priority patent/US8222463B2/en
Priority claimed from US13/193,007 external-priority patent/US20110312488A1/en
Application filed by UOP LLC filed Critical UOP LLC
Publication of WO2013015996A2 publication Critical patent/WO2013015996A2/fr
Publication of WO2013015996A3 publication Critical patent/WO2013015996A3/fr
Anticipated expiration legal-status Critical
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/153—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the catalyst used
    • C07C29/156—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the catalyst used containing iron group metals, platinum group metals or compounds thereof
    • C07C29/157—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the catalyst used containing iron group metals, platinum group metals or compounds thereof containing platinum group metals or compounds 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
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/888—Tungsten
    • 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
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/14—Phosphorus; Compounds thereof
    • B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J27/188—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with chromium, molybdenum, tungsten or polonium
    • 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
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • the invention relates to a catalyst system and process for generating at least one polyol from a feedstock comprising at least one saccharide using the specific catalyst system,
  • the process involves, contacting hydrogen, water, and the feedstock comprising saccharide, with a catalyst system to generate an effluent comprising at least one polyol and recovering the polyol from the effluent.
  • the catalyst system comprises both a metal component with an oxidation state greater than or equal to 2+ and a hydrogenation component.
  • Polyols are valuable materials that find use in the manufacture of cold weather fluids, cosmetics, polyesters and many other synthetic products. Generating polyols from saccharides instead of fossil fuel-derived olefins can be a more environmentally friendly and a more economically attractive process. Previously, polyols have been generated from polyhydroxy compounds, see WO 2006/092085 and US 2004/0175806. Recently, catalytic conversion of saccharide into ethylene glycol over supported carbide catalysts was disclosed in Catalysis Today, 147, (2009) 77-85.
  • US 2010/0256424, US 2010/0255983, and WO 2010/060345 teach a method of preparing ethylene glycol from saccharide and a tungsten carbide catalyst to catalyze the reaction.
  • Tungsten carbide catalysts have also been published as successful for batch-mode direct catalytic conversion of saccharide to ethylene glycol in Angew. Chem. Int. Ed 2008, 47, 8510-8513 and supporting information.
  • a small amount of nickel was added to a tungsten carbide catalyst in Chem. Comm. 2010, 46, 862-864.
  • Bimetallic catalysts have been disclosed in ChemSusChem, 2010, 3, 63-66. Additional references disclosing catalysts known in the art for the direct conversion of cellulose to ethylene glycol or propylene glycol include WO2010/060345; US 7,767,867; Chem.
  • the process and catalyst system comprising at least one metal component (Ml) selected from IUPAC Group 4, 5 or 6 of the periodic table with an oxidation state greater than or equal to 2+ and at least one hydrogenation component (M2) selected from IUPAC Group 8, 9, or 10 of the periodic table for generating at least one polyol from a feedstock comprising at least one saccharide described herein addresses this need.
  • the metal component (Ml) is in a form other than a carbide, nitride or phosphide.
  • One embodiment of the invention is a catalyst system useful for the conversion of at least one saccharide to polyol, the catalyst system comprising a metal component with an oxidation state greater than or equal to 2+ (Ml) and a hydrogenation component (M2).
  • the metal component Ml is selected from IUPAC Groups 4, 5 and 6 of the Periodic table
  • the hydrogenation component (M2) is selected from the group consisting of IUPAC Groups 8, 9, and 10 of the Periodic Table.
  • the metal component (Ml) may be selected from the group consisting of tungsten, molybdenum, vanadium, niobium, chromium, titanium, zirconium and any combination thereof.
  • the metal component may be comprised within a compound.
  • the metal component is in a form other than a carbide, nitride, or phosphide
  • the hydrogenation component may comprise, for example, an active metal component selected from the group comprising Pt, Pd, Ru, Rh, Ni, Ir, and combinations thereof.
  • Ml, M2 or both Ml and M2 may be unsupported or supported on a solid catalyst support.
  • the solid catalyst support is selected from the group consisting of carbon, A1 2 0 3 , Zr0 2 , Si0 2 , MgO, Ce x ZrO y , Ti0 2 , SiC, silica alumina, zeolites, clays and combinations thereof.
  • the mass ratio of Ml to M2, on an elemental basis ranges from 1 : 100 to 100: 1.
  • the Ml component, M2 component, or both the Ml and M2 components comprises from 0.05 to 30 mass percent, on an elemental basis of the supported catalyst.
  • Measurements of the metal component and the hydrogenation component such as mass ratios, weight ratios, and mass percents are provided herein on an elemental basis with respect to the IUPAC Groups 4, 5 and 6 and IUPAC Groups 8, 9, and 10 elements of the Periodic Table.
  • Another embodiment of the invention is a process for generating at least one polyol from a feedstock comprising at least one saccharide where the process comprises contacting hydrogen, water, and feedstock with a catalyst system to generate an effluent comprising at least one polyol, and recovering the polyol from the effluent.
  • the process may be operated in a batch mode operation or in a continuous mode operation.
  • the catalyst system comprises a metal component (Ml) having an oxidation state greater than or equal to 2+ and a
  • the metal component Ml is selected from IUPAC Groups 4, 5 and 6 of the Periodic table, and the hydrogenation component (M2) is selected from the group consisting of IUPAC Groups 8, 9, and 10 of the Periodic Table.
  • the metal component (Ml) may be selected from the group consisting of tungsten, molybdenum, vanadium, niobium, chromium, titanium, zirconium and any combination thereof.
  • the metal component may be comprised within a compound.
  • the metal component is in a form other than a carbide, nitride, or phosphide
  • the hydrogenation component may comprise an active metal component selected from the group comprising Pt, Pd, Ru, Rh, Ni, Ir, and combinations thereof.
  • the hydrogenation component may be comprised within a compound.
  • M2 or both Ml and M2 may be unsupported or supported on a solid catalyst support.
  • the solid catalyst support is selected from the group consisting of carbon, A1 2 0 3 , Zr0 2 , Si0 2 , MgO, Ce x ZrO y , Ti0 2 , SiC, silica alumina, zeolites, clays and combinations thereof.
  • the mass ratio of Ml to M2 ranges from 1 : 100 to 100: 1 on an elemental basis. If supported, the Ml component, M2 component, or both the Ml and M2 components comprises from 0.05 to 30 mass percent, on an elemental basis, of the supported catalyst.
  • Yet another embodiment of the invention is a continuous process for generating at least one polyol from a feedstock comprising at least one saccharide.
  • the process involves, contacting, in a continuous manner, hydrogen, water, and a feedstock comprising at least one saccharide, with a catalyst system to generate an effluent stream comprising at least one polyol and recovering the polyol from the effluent stream.
  • the hydrogen, water, and feedstock are fed to the reactor in a continuous manner.
  • the effluent stream is removed from the reactor in a continuous manner.
  • the process is a catalytic process employing a catalyst system comprising a metal component (Ml) having an oxidation state greater than or equal to 2+ and a hydrogenation component (M2) as described above.
  • the contacting occurs in a reaction zone having at least a first input stream and a second input stream, the first input stream comprising at least the feedstock comprising at least one saccharide and the second input stream comprising hydrogen.
  • the first input stream may be pressurized prior to the reaction zone and the second input stream may be pressurized and heated prior to the reaction zone.
  • the first input stream may be pressurized and heated to a temperature below the thermal decomposition
  • the temperature of the saccharide prior to the reaction zone and the second input stream may be pressurized and heated prior to the reaction zone.
  • the first input stream and the second input stream further comprise water.
  • the polyol produced is at least ethylene glycol or propylene glycol.
  • Co-products such as alcohols, organic acids, aldehydes, monosaccharides, disaccharides, oligosaccharides, polysaccharides, phenolic compounds, hydrocarbons, glycerol, depolymerized lignin, and proteins may also be generated.
  • the feedstock may be treated prior to contacting with the catalyst by a technique such as sizing, drying, grinding, hot water treatment, steam treatment, hydrolysis, pyrolysis, thermal treatment, chemical treatment, biological treatment, catalytic treatment, or combinations thereof.
  • the effluent stream from the reactor system may further comprise catalyst which may be separated from the effluent stream using a technique such as direct filtration, settling followed by filtration, hydrocyclone, fractionation, centrifugation, the use of flocculants, precipitation, liquid extraction, adsorption, evaporation, and combinations thereof.
  • catalyst which may be separated from the effluent stream using a technique such as direct filtration, settling followed by filtration, hydrocyclone, fractionation, centrifugation, the use of flocculants, precipitation, liquid extraction, adsorption, evaporation, and combinations thereof.
  • FIG. 1 is a basic diagram of the flow scheme of one embodiment of the invention. Equipment and processing steps not required to understand the invention are not depicted.
  • FIG. 2 is a basic diagram of the flow scheme of another embodiment of the invention showing an optional pretreatment zone and an optional supported catalyst component separation zone with optional supported catalyst component recycle. Equipment and processing steps not required to understand the invention are not depicted. DETAILED DESCRIPTION OF THE INVENTION
  • the invention involves a catalyst system and a process for generating at least one polyol from a feedstock comprising at least one saccharide.
  • the catalyst system comprises metal component (Ml) with an oxidation state greater than or equal to 2+ and a
  • the metal component (Ml) is selected from IUPAC Groups 4, 5 and 6 of the Periodic table.
  • the metal component (Ml) may be selected from the group consisting of tungsten, molybdenum, vanadium, niobium, chromium, titanium, zirconium and any combination thereof.
  • the metal component may be comprised within a compound.
  • the metal component is not in the form of a carbide, nitride, or phosphide.
  • the hydrogenation component (M2) is selected from the group consisting of IUPAC Groups 8, 9, and 10 of the Periodic Table.
  • the hydrogenation component may be comprised within a compound.
  • the hydrogenation component may comprise an active metal component selected from the group comprising Pt, Pd, Ru, Rh, Ni, Ir, and combinations thereof.
  • Ml, M2 or both Ml and M2 may be unsupported or supported on a solid catalyst support.
  • the solid catalyst support is selected from the group consisting of carbon, A1 2 0 3 , Zr0 2 , Si0 2 , MgO, Ce x ZrO y , Ti0 2 , SiC, silica alumina, zeolites, clays and combinations thereof.
  • the mass ratio of Ml to M2 ranges from 1 : 100 to 100: 1 on an elemental basis.
  • the Ml component, M2 component, or both the Ml and M2 components comprises from 0.05 to 30 mass percent, on an elemental basis, of the supported catalyst.
  • Measurements of the metal component and the hydrogenation component such as mass ratios, weight ratios, and mass percents are provided herein on an elemental basis with respect to the IUPAC Groups 4, 5 and 6 and IUPAC Groups 8, 9, and 10 elements of the Periodic Table.
  • the process involves contacting, hydrogen, water, and a feedstock comprising at least one saccharide, with the catalyst system described above to generate an effluent comprising at least one polyol, and recovering the polyol from the effluent.
  • the process may be operated in a batch mode operation or in a continuous mode operation.
  • the process involves continuous catalytic conversion of a flowing stream of feedstock comprising saccharide to ethylene glycol or propylene glycol with high yield and high selectivity.
  • the feedstock comprises at least one saccharide which may be any class of monosachharides, disaccharides, oligosachharides, and polysachharides and may be edible, inedible, amorphous or crystalline in nature.
  • the feedstock comprises polysaccharides that consist of one or a number of monosaccharides joined by glycosidic bonds. Examples of polysaccharides include glycogen, cellulose, hemicellulose, starch, chitin and combinations thereof.
  • saccharide may be any class of monosachharides, disaccharides, oligosachharides, and polysachharides and may be edible, inedible, amorphous or crystalline in nature.
  • the feedstock comprises polysaccharides that consist of one or a number of monosaccharides joined by glycosidic bonds. Examples of polysaccharides include glycogen, cellulose, hemicellulose, starch, chitin and combinations thereof.
  • saccharide as used herein is meant to
  • saccharide is cellulose, hemicellulose, or a combination thereof.
  • Hemicellulose is generally understood to be any of several polysaccharides that are more complex than a sugar.
  • cellulose and hemicellulose are large renewable resources having a variety of attractive sources, such as residue from agricultural production or waste from forestry or forest products. Since cellulose and hemicellulose cannot be digested by humans, using cellulose and or hemicellulose as a feedstock does not take from our food supply.
  • cellulose and hemicellulose can be a low cost waste type feedstock material which is converted herein to high value products like polyols such as ethylene glycol and propylene glycol.
  • the feedstock comprising saccharide of the process may be derived from sources such as agricultural crops, forest biomass, waste material, recycled material.
  • sources such as agricultural crops, forest biomass, waste material, recycled material.
  • Examples include short rotation forestry, industrial wood waste, forest residue, agricultural residue, energy crops, industrial wastewater, municipal wastewater, paper, cardboard, fabrics, pulp derived from biomass, corn starch, sugarcane, grain, sugar beet, glycogen and other molecules comprising the molecular unit structure of C m (H 2 0) n , and combinations thereof.
  • the feedstock may be whole biomass including cellulose, lignin and hemicellulose or treated biomass where the polysaccharide is at least partially depolymerized, or where the lignin, hemicelluUose or both have been at least partially removed from the whole biomass.
  • the feedstock may be continuously contacted with the catalyst system in a reactor system such as an ebullating catalyst bed reactor system, an immobilized catalyst reactor system having catalyst channels, an augured reactor system, fluidized bed reactor systems, mechanically mixed reactor systems, slurry reactor systems, also known as a three phase bubble column reactor systems, and
  • a reactor system such as an ebullating catalyst bed reactor system, an immobilized catalyst reactor system having catalyst channels, an augured reactor system, fluidized bed reactor systems, mechanically mixed reactor systems, slurry reactor systems, also known as a three phase bubble column reactor systems, and
  • Examples of operating conditions in the rector system include temperatures ranging from 100°C to 350°C and hydrogen pressures greater than 150 psig. In one embodiment, the temperature in the reactor system may range from 150°C to 350°C, in another embodiment the temperature in the reactor system may range from 200°C to 280°C.
  • the feedstock which comprises at least one saccharide, may be continuously contacted with the catalyst system in the reactor system at a water to feedstock weight ratio ranging from 1 to 100, a catalyst (M1+M2) to feedstock weight ratio of greater than 0.005, a pH of less than 10 and a residence time of greater than five minutes. In another embodiment, the catalyst to feedstock weight ratio is greater than 0.01.
  • the process of the invention maybe operated in a batch mode operation, or may be operated in a continuous mode of operations.
  • a batch mode operation the necessary reactants and catalyst system are combined and allowed to react. After a period of time, the reaction mixture is removed from the reactor and separated to recover products.
  • Autoclave reactions are common examples of batch reactions. While the process may be operated in the batch mode, there are advantages to operating in the continuous mode, especially in larger scale operations. The following description will focus on continuous mode operation, although the focus of the following description does not limit the scope of the invention.
  • the feedstock is continually being introduced into the reaction zone as a flowing stream and a product comprising a polyol is being continuously withdrawn.
  • Materials must be capable of being transported from a low pressure source into the reaction zone, and products must be capable of being transported from the reaction zone to the product recovery zone.
  • residual solids if any, must be capable of being removed from the reaction zone.
  • a challenge in processing a feedstock comprising saccharide in a pressurized hydrogen environment is that the feedstock may be an insoluble solid. Therefore, pretreatment of the feedstock may be performed in order to facilitate the continuous transporting of the feedstock. Suitable pretreatment operations may include sizing, drying, grinding, hot water treatment, steam treatment, hydrolysis, pyrolysis, thermal treatment, chemical treatment, biological treatment, catalytic treatment, and combinations thereof. Sizing, grinding or drying may result in solid particles of a size that may be flowed or moved through a continuous process using a liquid or gas flow, or mechanical means.
  • An example of a chemical treatment is mild acid hydrolysis of polysaccharide.
  • catalytic treatments are catalytic hydrolysis of polysaccharide, catalytic hydrogenation of
  • polysaccharide or both, and an example of biological treatment is enzymatic hydrolysis of polysaccharide.
  • Hot water treatment, steam treatment, thermal treatment, chemical treatment, biological treatment, or catalytic treatment may result in lower molecular weight saccharides and depolymerized lignins that are more easily transported as compared to the untreated polysaccharide.
  • Suitable pretreatment techniques are found in "Catalytic Hydrogenation of Corn Stalk to Ethylene Glycol and 1 ,2-Propylene Glycol" Jifeng Pang, Mingyuan Zheng, Aiqin Wang, and Tao Zhang Ind. Eng. Chem. Res. DOI: 10.1021/iel02505y, Publication Date (Web): April 20, 2011. See also, US 2002/0059991.
  • the saccharide is thermally sensitive. Exposure to excessive heating prior to contacting with the catalyst may result in undesired thermal reactions of the saccharide such as charring of the saccharide.
  • the feedstock comprising saccharide is provided to the reaction zone containing the catalyst in a separate input stream from the primary hydrogen stream.
  • the reaction zone has at least two input streams.
  • the first input stream comprises at least the feedstock comprising saccharide
  • the second input stream comprises at least hydrogen. Water may be present in the first input stream, the second input stream or in both input streams. Some hydrogen may also be present in the first input stream with the feedstock comprising saccharide.
  • the hydrogen stream may be heated in excess of the reaction temperature without also heating the feedstock comprising saccharide to reaction temperature.
  • the temperature of first input stream comprising at least the feedstock comprising saccharide may be controlled not to exceed the temperature of unwanted thermal side reactions.
  • the temperature of first input stream comprising at least the feedstock comprising saccharide may be controlled not to exceed the decomposition temperature of the saccharide or the charring temperature of the saccharide.
  • the first input stream, the second input stream, or both may be pressurized to reaction pressure before being introduced to the reaction zone.
  • the feedstock comprising saccharide is continuously introduced to a catalytic reaction zone as a flowing stream.
  • Water and hydrogen, both reactants are present in the reaction zone.
  • at least a portion of the hydrogen may be introduced separately and independent from the feedstock comprising saccharide, or any combination of reactants, including feedstock comprising saccharide, may be combined and introduced to the reaction zone together. Because of the mixed phases likely to be present in the reaction zone specific types of reactor systems are preferred.
  • suitable reactor systems include ebullating catalyst bed reactor systems, immobilized catalyst reactor systems having catalyst channels, augured reactor systems, fluidized bed reactor systems, mechanically mixed reactor systems and slurry reactor systems, also known as a three phase bubble column reactor systems, and combinations thereof.
  • metallurgy of the reactor system is selected to be compatible with the reactants and the desired products within the range of operating conditions.
  • suitable metallurgy for the reactor system include titanium, zirconium, stainless steel, carbon steel having hydrogen embrittlement resistant coating, carbon steel having corrosion resistant coating.
  • the metallurgy of the reaction system includes either coated or clad carbon steel.
  • the reactants proceed through catalytic conversion reactions to produce at least one polyol.
  • Desired polyols include ethylene glycol and propylene glycol.
  • Co-products may also be produced and include compounds such as alcohols, organic acids, aldehydes, monosaccharides, polysaccharides, phenolic compounds, hydrocarbons, glycerol, depolymerized lignin and proteins.
  • the co-products may have value and may be recovered in addition to the product polyols.
  • the reactions may proceed to completion, or some reactants and intermediates may remain in a mixture with the products.
  • Intermediates which are included herein as part of the co-products, may include compounds such as depolymerized cellulose, lignin and hemicellulose. Unreacted hydrogen, water, and polysaccharide may also be present in the reaction zone effluent along with products and co-products. Unreacted material and or intermediates may be recovered and recycled to the reaction zone.
  • the reactions are catalytic reactions and the reaction zone comprises at least one catalyst system where the catalyst system comprises a metal component with an oxidation state greater than or equal to 2+ (Ml) and a hydrogenation component (M2).
  • the metal component Ml is selected from IUPAC Groups 4, 5 and 6 of the Periodic table
  • the hydrogenation component (M2) is selected from the group consisting of IUPAC Groups 8, 9, and 10 of the Periodic Table.
  • the catalyst system may also be considered a multi-component catalyst, and the terms are used herein interchangeably.
  • the metal component (Ml) may be present in the catalyst system in any catalytically available form that has the metal component in an oxidation state greater than or equal to 2+.
  • the metal component may be in a compound or may be in chemical combination with one or more of the other ingredients of the catalyst system.
  • the metal component (Ml) may be selected from the group consisting of tungsten, molybdenum, vanadium, niobium, chromium, titanium, zirconium and any combination thereof.
  • the metal component may be comprised within a compound.
  • the metal component is in a form other than a carbide, nitride, or phosphide.
  • Compounds comprising the Ml component of the catalyst system may be selected from the group consisting of tungstic acid, molybedic acid, ammonium tungstate, ammonium metatungstate, ammonium paratungstate, tungstate compounds comprising at least one Group I or II element, metatungstate compounds comprising at least one Group I or II element, paratungstate compounds comprising at least one Group I or II element, heteropoly compounds of tungsten, heteropoly compounds of molybdenum, tungsten oxides, molybdenum oxides, vanadium oxides, metavanadates, chromium oxides, chromium sulfate, titanium ethoxide, zirconium acetate, zirconium carbonate, zirconium hydroxide, niobium oxides, niobium ethoxide, and combinations thereof.
  • the metal component is in a form other than a carbide, nitride, or phosphide.
  • the hydrogenation component (M2) may be present in the catalyst system in any catalytically available form.
  • the hydrogenation component may be in the elemental form or may be a compound or may be in chemical combination with one or more of the other ingredients of the catalyst system.
  • the hydrogenation component may comprise an active metal component selected from the group comprising Pt, Pd, Ru, Rh, Ni, Ir, and combinations thereof.
  • the metal component Ml, the hydrogenation component M2 or both Ml and M2 may be unsupported or supported on one or more solid catalyst supports. Refractory oxide catalyst supports and others may be used.
  • the mass ratio of Ml to M2, on an elemental basis, ranges from 1 : 100 to 100: 1. If supported, the Ml component, M2 component, or both the Ml and M2 components comprises from 0.05 to 30 mass percent, on an elemental basis, of the supported catalyst.
  • the description below generally refers to the catalyst support. Such general description to the catalyst support is not meant to limit the broad scope of the invention to a single catalyst support. For example in one embodiment Ml is supported on a first catalyst support and M2 is supported on a second catalyst support and the first catalyst support and the second catalyst support may be the same composition or different
  • the support may be in the shape of a powder, or specific shapes such as spheres, extrudates, pills, pellets, tablets, irregularly shaped particles, monolithic structures, catalytically coated tubes, or catalytically coated heat exchanger surfaces.
  • the refractory inorganic oxide supports include but are not limited to silica, aluminas, silica- alumina, titania, zirconia, magnesia, clays, zeolites, molecular sieves, etc. It should be pointed out that silica-alumina is not a mixture of silica and alumina but means an acidic and amorphous material that has been cogelled or coprecipitated. Carbon and activated carbon may also be employed as supports.
  • suitable supports include carbon, activated carbon, A1 2 0 3 , Zr0 2 , Si0 2 , MgO, Ce x ZrO y , Ti0 2 , SiC, silica alumina, zeolites, clays and combinations thereof.
  • combinations of materials can be used as the support.
  • Ml, M2, or the combination of Ml and M2 may be incorporated onto the catalytic support in any suitable manner known in the art, such as by coprecipitation, coextrusion with the support, or impregnation.
  • Ml, M2, or the combination of Ml and M2 may comprise from 0.05 to 30 mass %, on an elemental basis, of the supported catalyst.
  • Ml, M2, or the combination of Ml and M2 may comprise from 0.3 to 15 mass %, on an elemental basis, of the supported catalyst. In still another embodiment, Ml, M2, or the combination of Ml and M2 may comprise from 0.5 to 7 mass %, on an elemental basis, of the supported catalyst.
  • the relative amount of Ml catalyst component to M2 catalyst component may range from 1 : 100 to 100: 1 as measured by ICP or other common wet chemical analysis methods. In another embodiment, the relative amount of Ml catalyst component to M2 catalyst component may range from 1 :20 to 50: 1 , and in still another embodiment, the relative amount of Ml catalyst component to M2 catalyst component may range from 1 : 10 to 10: 1.
  • the amount of the catalyst system used in the process may range from 0.005 to 0.4 mass % of the feedstock comprising saccharide. In other embodiment, the amount of the catalyst system used in the process may range from 0.01 to 0.25 mass % of the feedstock comprising saccharide. In still other embodiment, the amount of the catalyst system used in the process may range from 0.02 to 0.15 mass % of the feedstock comprising saccharide.
  • the reactions occurring are multistep reactions and different amounts of the catalyst system, or relative amounts of the components of the catalyst system, can be used to control the rates of the different reactions. Individual applications may have differing requirements as to the amounts of the catalyst system, or relative amounts of the components of the catalyst system used.
  • the Ml catalyst component may be a solid that is soluble in the reaction mixture, or at least partially soluble in the reaction mixture which includes at least water and the feedstock at reaction conditions.
  • An effective amount of the solid Ml catalyst should be soluble in the reaction mixture. Different applications and Ml catalyst components will result in differing effective amounts of Ml catalyst component needed to be in solution in the reaction mixture.
  • the Ml catalyst component is miscible or at least partially miscible with the reaction mixture.
  • an effective amount of the liquid Ml catalyst should be miscible in the reaction mixture.
  • different applications and different Ml catalyst components will result in differing effective amounts of Ml catalyst component needed to be miscible in the reaction mixture.
  • the amount of Ml catalyst component miscible in water is in the range of 1 to 100 %, in another embodiment, from 10 to 100 %, and in still another embodiment, from 20 to 100 %.
  • the multicomponent catalyst of the present invention may provide several advantages over a more traditional single component catalyst. For example, in some embodiments, the manufacture costs of the catalyst may be reduced since fewer active components need to be incorporated onto a solid catalyst support. Operational costs may be reduced since it is envisioned that less catalyst make-up will be required and more selective processing steps can be used for recovery and recycle of catalyst. Other advantages include improved catalyst stability which leads to lower catalyst consumption and lower cost per unit of polyol product, and the potential for improved selectivity to ethylene glycol and propylene glycol with reduced production of co-boiling impurities such as butane diols.
  • the catalyst system may be contained within the reaction zone, and in other embodiments the catalyst may continuously or intermittently pass through the reaction zone, and in still other embodiments, the catalyst system may do both, with at least one catalyst system component residing in a reaction zone while the other catalyst system component continuously or intermittently passes through the reaction zone.
  • Suitable reactor systems include an ebullating catalyst bed reactor system, an immobilized catalyst reactor system having catalyst channels, an augured reactor system, a fluidized bed reactor system, a mechanically mixed reactor systems, a slurry reactor system, also known as a three phase bubble column reactor system and combinations thereof.
  • Examples of operating conditions in the rector system include temperatures ranging from 100°C to 350°C and hydrogen pressures greater than 150 psig.
  • the temperature in the reactor system may range from 150°C to 350°C, in another embodiment the temperature in the reactor system may range from 200°C to 280°C.
  • the feedstock which comprises at least one saccharide, may be continuously contacted with the catalyst system in the reactor system at a water to feedstock weight ratio ranging from 1 to 100, a catalyst (M1+M2) to feedstock weight ratio of greater than 0.005, a pH of less than 10 and a residence time of greater than 5 minutes.
  • the water to feedstock weight ratio ranges from 1 to 20 and the catalyst to feedstock weight ratio is greater than 0.01.
  • the water to feedstock weight ratio ranges from 1 to 5 and the catalyst to feedstock weight ratio is greater than 0.1.
  • the catalytic reaction system employs a slurry reactor.
  • Slurry reactors are also known as three phase bubble column reactors.
  • Slurry reactor systems are known in the art and an example of a slurry reactor system is described in US
  • the catalyst system may be mixed with the water and feedstock comprising saccharide to form a slurry which is conducted to the slurry reactor.
  • the reactions occur within the slurry reactor and the catalyst is transported with the effluent stream out of the reactor system.
  • the slurry reactor system may be operated at conditions listed above.
  • the catalytic reaction system employs an ebullating bed reactor. Ebullating bed reactor systems are known in the art and an example of an ebullating bed reactor system is described in US 6,436,279.
  • the effluent stream from the reaction zone contains at least the product polyol(s) and may also contain unreacted water, hydrogen, saccharide, byproducts such as phenolic compounds and glycerol, and intermediates such as depolymerized polysaccharides and lignins.
  • the effluent stream may also contain at least a portion of the catalyst system.
  • the effluent stream may contain a portion of the catalyst system that is in the liquid phase, or a portion of the catalyst system that is in the solid phase. In some embodiments it may be advantageous to remove solid phase catalyst components from the effluent stream, either before or after and desired products or by-products are recovered.
  • Solid phase catalyst components may be removed from the effluent stream using one or more techniques such as direct filtration, settling followed by filtration, hydrocyclone, fractionation, centrifugation, the use of flocculants, precipitation, extraction, evaporation, or combinations thereof.
  • one or more techniques such as direct filtration, settling followed by filtration, hydrocyclone, fractionation, centrifugation, the use of flocculants, precipitation, extraction, evaporation, or combinations thereof.
  • separated catalyst may be recycled to the reaction zone.
  • the catalyst system, water, and feedstock comprising saccharide are conducted via stream 122 to reaction zone 124.
  • the mixture in stream 122 has, for example, a water to feedstock comprising saccharide weight ratio of 5 and a catalyst system to feedstock comprising saccharide weight ratio of 0.05.
  • At least hydrogen is conducted via stream 125 to reaction zone 124.
  • Reaction zone 124 is operated, for example, at a temperature of 250°C a hydrogen pressure of 1200 psig, a pH of 7 and a residence time of 8 minutes.
  • reaction zone 124 Prior to introduction into reaction zone 124, the catalyst, water, and feedstock comprising saccharide in stream 122 and the hydrogen in stream 125 are brought to a pressure of 1800 psig to be at the same pressure as reaction zone 124. However, only stream 125 comprising at least hydrogen is raised to at least 250°C to be at a temperature greater than or equal to the temperature in reaction zone 124.
  • the mixture in stream 122 which contains at least the saccharide is temperature controlled to remain at a temperature lower than the decomposition or charring temperature of the saccharide.
  • the saccharide is catalytically converted into at least ethylene glycol or propylene glycol.
  • Reaction zone effluent 126 contains at least the product ethylene glycol or propylene glycol.
  • Reaction zone effluent 126 may also contain alcohols, organic acids, aldehydes, monosaccharides, polysaccharides, phenolic compounds, hydrocarbons, glycerol, depolymerized lignin, and proteins.
  • Reaction zone effluent 126 is conducted to product recovery zone 134 where the desired glycol products are separated and recovered in steam 136. Remaining components of reaction zone effluent 126 are removed from product recovery zone 134 in stream 138.
  • water and feedstock comprising polysaccharide 210 is introduced to pretreatment unit 220 where the saccharide is ground to a particle size that is small enough to be pumped as a slurry with the water using conventional equipment.
  • the pretreated feedstock is combined with water in line 219 and catalyst system in line 223 and combined stream 227 is conducted to reaction zone 224.
  • the combined stream 227 has, for example, a water to feedstock comprising saccharide weight ratio of 20 and a catalyst system to saccharide weight ratio of 0.1.
  • At least hydrogen is conducted via stream 225 to reaction zone 224. Some hydrogen may be combined with stream 227 prior to reaction zone 224 as shown by optional dotted line 221.
  • Reaction zone 224 is operated, for example, at a temperature of 280°C a hydrogen pressure of 200 psig, a pH of 7 and a residence time of 8 minutes.
  • the catalyst system, water, and pretreated feedstock comprising saccharide in stream 227 and the hydrogen in stream 225 Prior to introduction into reaction zone 224, the catalyst system, water, and pretreated feedstock comprising saccharide in stream 227 and the hydrogen in stream 225 are brought to a pressure of 1800 psig to be at the same temperature as reaction zone 224.
  • stream 225 comprising at least hydrogen is raised to at least 250°C to be at a temperature greater than or equal to the temperature of reaction zone 224.
  • the mixture in stream 227 which contains at least the saccharide is temperature controlled to remain at a temperature lower than the decomposition or charring temperature of the polysaccharide.
  • the saccharide is catalytically converted into at least ethylene glycol or polyethylene glycol.
  • Reaction zone effluent 226 contains at least the product ethylene glycol or propylene glycol and catalyst. Reaction zone effluent 226 may also contain alcohols, organic acids, aldehydes, monosaccharides, polysaccharides, phenolic compounds, hydrocarbons, glycerol, depolymerized lignin, and proteins. Reaction zone effluent 226 is conducted to optional catalyst system recovery zone 228 where catalyst components are separated from reaction zone effluent 226 and removed in line 232. Catalyst components in line 232 may optionally be recycled to combine with line 223 or to reaction zone 224 as shown by optional dotted line 229.
  • the catalyst component-depleted reaction zone effluent 230 is conducted to product recovery zone 234 where the desired glycol products are separated and recovered in steam 236. Remaining components of effluent 230 are removed from product recovery zone 234 in stream 238.
  • Microcrystalline cellulose was obtained from Sigma- Aldrich.
  • Ni on Norit CA-1 catalyst was prepared by impregnating various amounts of Ni using Ni nitrate in water onto activated carbon support Norit-CAl using incipient wetness technique. The impregnated support was then dried at 40°C overnight in an oven with nitrogen purge and reduced in H2 at 750°C for 1 hrs.
  • 5%Pd/C and 5%Pt/C were purchased from Johnson Matthey. Ethylene glycol and propylene glycol yields were measured as mass of ethylene glycol or propylene glycol produced divided by the mass of feedstock used and multiplied by 100.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Saccharide Compounds (AREA)

Abstract

L'invention porte sur un procédé d'obtention d'au moins un polyol, à partir d'une charge de départ comportant un saccharide, effectué d'une manière continue ou discontinue à l'aide d'un système catalyseur. Le procédé comprend la mise en contact d'hydrogène, d'eau et d'une charge de départ comportant un saccharide avec un système catalyseur pour produire un courant d'effluent comportant au moins un polyol et la récupération du polyol dans le courant d'effluent. Le système catalyseur comporte au moins un composant métallique à un état d'oxydation supérieur ou égal à 2+.
PCT/US2012/046342 2011-07-28 2012-07-12 Obtention de polyols à partir d'une charge de départ contenant des saccharides Ceased WO2013015996A2 (fr)

Applications Claiming Priority (4)

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US13/193,072 2011-07-28
US13/193,007 2011-07-28
US13/193,072 US8222463B2 (en) 2011-07-28 2011-07-28 Process for generation of polyols from saccharide containing feedstock
US13/193,007 US20110312488A1 (en) 2011-07-28 2011-07-28 Catalyst system for generation of polyols from saccharide containing feedstock

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WO2016001169A1 (fr) * 2014-06-30 2016-01-07 Haldor Topsøe A/S Procédé pour la préparation d'éthylène glycol à partir de sucres
WO2017055285A1 (fr) * 2015-09-29 2017-04-06 Shell Internationale Research Maatschappij B.V. Procédé pour la préparation de glycols

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WO2016001169A1 (fr) * 2014-06-30 2016-01-07 Haldor Topsøe A/S Procédé pour la préparation d'éthylène glycol à partir de sucres
KR20170027778A (ko) * 2014-06-30 2017-03-10 할도르 토프쉐 에이/에스 당으로부터 에틸렌글리콜을 제조하는 방법
US10077222B2 (en) 2014-06-30 2018-09-18 Haldor Topsoe A/S Process for the preparation of ethylene glycol from sugars
AU2015282666B2 (en) * 2014-06-30 2019-04-18 Haldor Topsoe A/S Process for the preparation of ethylene glycol from sugars
TWI660936B (zh) * 2014-06-30 2019-06-01 丹麥商托普索公司 從糖製備乙二醇的方法
KR102044453B1 (ko) 2014-06-30 2019-11-13 할도르 토프쉐 에이/에스 당으로부터 에틸렌글리콜을 제조하는 방법
WO2017055285A1 (fr) * 2015-09-29 2017-04-06 Shell Internationale Research Maatschappij B.V. Procédé pour la préparation de glycols

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