Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07D—HETEROCYCLIC COMPOUNDS
  • C07D307/00—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom
  • C07D307/02—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings
  • C07D307/34—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members
  • C07D307/38—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members with substituted hydrocarbon radicals attached to ring carbon atoms
  • C07D307/40—Radicals substituted by oxygen atoms
  • C07D307/46—Doubly bound oxygen atoms, or two oxygen atoms singly bound to the same carbon atom
• • 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
  • B01J21/18—Carbon
• • 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
  • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
• • 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
  • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
  • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
• • 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
  • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
  • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
  • B01J23/42—Platinum

Definitions

• the present invention relates to a process for preparing furan-2,5-dicarboxylic acid (FDCA) (compound of the formula (I)) and to a corresponding use of a catalyst.
• FDCA furan-2,5-dicarboxylic acid
• FDCA is an important compound for production of various products, for example surfactants, polymers and resins.
• PET polyethylene terephalate
• terephthalic acid a compound used in the production of polyethylene terephalate, PET
• PET is based on ethylene and p-xylene which are usually obtained starting from of oil, natural gas or coal, i.e. from fossil fuels.
• bio-based routes to ethylene e.g. dehydration of bio-ethanol
• FDCA is the best bio-based alternative to terephthalic acid (for further information see: Lichtenthaler, F. W., “ Carbohydrates as Organic Raw Materials ” in Ullmann's Encyclopedia of Industrial Chemistry, Wiley-VCH Verlag GmbH & Co. KGaA, Weinheim, 2010).
• FDCA can be co-polymerized with mono-ethylene glycol to give polyethylene furanoate (PEF), a polyester with properties similar to PET.
• PET polyethylene furanoate
• FDCA is usually obtained starting from fructose and/or other hexoses via a catalyzed, preferably acid-catalyzed, dehydration to key intermediate 5-(hydroxymethyl)furfural (HMF) followed by oxidation to FDCA.
• HMF 5-(hydroxymethyl)furfural
• a typical by-product is 5,5′-[oxy-bis(methylene)]bis-2-furfural (di-HMF) (V, see below).
• a starting mixture comprising 5-(hydroxymethyl)furfural (HMF) is prepared by subjecting a material mixture, comprising one, two or more compounds selected from the group consisting of hexoses (monomeric hexose molecules, e.g. fructose), oligosaccharides comprising hexose units, and polysaccharides comprising hexose units, to reaction conditions so that a mixture comprising HMF, water and by-products (e.g. di-HMF) results. Under the reaction conditions oligo- and/or polysaccharides are usually depolymerised, and subsequently the resulting monosaccharides, e.g. monomeric hexose molecules, are converted into HMF. Hexoses, oligosaccharides and polysaccharides are typically selected from the group consisting of fructose, glucose, and cellulose.
• oligo- or polysaccharides are usually converted into monomeric hexose molecules by hydrolytic cleavage of the ether bonds connecting the different hexose units in an oligo- or polysaccharide molecule (e.g. cellulose).
• an oligo- or polysaccharide molecule e.g. cellulose
• the products of a typical depolymerization process are present in their aldehyde form.
• depolymerization is conducted by using a catalyst, preferably in a one-pot-procedure.
• a hydrophilic solvent is used (in particular water), e.g. in order to increase the amount of dissolved cellulose thus increasing the yield per process run.
• a heterogeneous catalyst in order to facilitate post-synthetic workup.
• an aqueous solution is used as a solvent, sometimes comprising 50 wt.-% of water or more, based on the total weight of the depolymerization mixture used.
• Monosaccharides produced or provided are typically subjected to a dehydration process, wherein the aldehyde form of monomeric hexose molecules is typically transferred by isomerization (via e.g. ketone-enone tautomerization) into its ketone form which is subsequently converted into its ring form.
• the formed ring-closed hexose molecules are typically dehydrated (and optionally further isomerized) resulting in a mixture comprising HMF, by-products (e.g. di-HMF) and water, which can be used as a basic mixture in a process for preparing FDCA (preferably in a purified form).
• the dehydration process step is usually performed in an aqueous environment so that an aqueous solution comprising HMF, by-products (e.g. di-HMF) and water is obtained as a (crude) mixture.
• HMF HMF often undergoes side-reactions, e.g. (further) etherification to di-HMF. This is usually the case when water is removed during work-up (see for example U.S. Pat. No. 2,994,645). Since two HMF-molecules are etherified the amount of by-products produced is correspondingly high.
• the (crude) mixture comprising HMF and water is usually contaminated with by-products, in particular di-HMF, to a certain degree, as separation of HMF from the by-products, in particular di-HMF, is not possible with justifiable effort.
• Common by-products are for example fructose in its ring form (RFF) (compound of the formula (III)), partially dehydrated fructose in its ring form (de-RFF) (compound of the formula (IV)), and 5,5′-[oxy-bis(methylene)]bis-2-furfural (di-HMF) (compound of the formula (V)).
• RMF fructose in its ring form
• de-RFF compound of the formula (IV)
• di-HMF 5,5′-[oxy-bis(methylene)]bis-2-furfural
• HMF compound of the formula (II)
• di-HMF can be obtained in significant amounts from biomass, especially from biomass comprising hexoses and/or oligo- and/or polysaccharides as described above.
• WO 2008/054804 A2 relates to “Hydroxymethyl furfural oxidation methods” (title). It is disclosed that a reaction mixture having a mild basic pH can be provided by addition of sodium carbonate, the salts of FDCA having a distinctly elevated solubility in said reaction mixture compared to reaction mixtures having a neutral or acidic pH (cf. paragraph [0049]).
• WO 2008/054804 A2 additionally discloses that twice as high a solubility of FDCA in an acetic acid/water mixture (volume ratio 40:60) is achieved, compared to the solubility in pure water (cf. paragraph [0058]).
• WO 2013/033081 A2 discloses a “process for producing both by-based succinic acid and 2,5-furane dicarboxylic acid” (title).
• title a mixture of HMF and di-HMF (molar ratio HMF:di-HMF is 1:10) is converted to FDCA at 100° C.
• US 2008/103318 discloses “hydroxymethyl furfural oxidation methods” (title) comprising the step of “providing a starting material which includes HMF in a solvent comprising water into reactor”. The starting material is brought into contact “with the catalyst comprising Pt on the support material where the contacting is conducted at a reaction temperature of from about 50° C. to about 200° C.”.
• WO 2012/017052 A1 discloses a “process for the synthesis of 2,5-furandicarboxylic acid” (title).
• Hicham Ait Rass et al. disclose a “selective aqueous phase oxidation of 5-hydroxymethyl furfural to 2,5-furandicarboxylic acid over Pt/C catalysts” (see atory of article in GREEN CHEMISTRY, vol. 15, no. 8, 1 Jan. 2013, page 2240).
• U.S. Pat. No. 2,994,645 discloses the “purification of hydroxymethyl furfural” (title). A process is disclosed wherein “gases and water by heating under a high vacuum” are initially removed.
• EP 0 356 703 A2 relates to a process for oxidizing 5-hydroxymethylfurfural (HMF) and discloses that the precipitation of reaction products during the oxidation of 5-hydroxymethylfurfural can be avoided, especially at relatively high concentrations, when a solubilizer which is inert with respect to the reaction participants under the selected reaction conditions is added to the reaction mixture.
• HMF 5-hydroxymethylfurfural
• suitable solubilizers are, for example, glycol ethers lacking free OH groups, especially dimethyl glycol ether, diethyl glycol ether and methyl ethyl glycol ether.
• WO 2013/191944 A1 discloses that, because of the very low solubility of FDCA in water, the oxidation of HMF has to be conducted in very dilute solutions, in order to avoid precipitation of the FDCA on the catalyst surface, since the process otherwise can no longer be conducted economically (cf. page 3).
• depolymerization or dehydration step also apply to (i) a process for preparing FDCA and (ii) a use of a catalyst according to the present invention as described in detail hereinbelow.
• the dehydration step or the successive steps of depolymerization and dehydration can be used to prepare a starting mixture as employed according to the present invention.
• this object is achieved by a process for preparing furane-2,5-dicarboxylic acid, comprising the following step:
• the “heterogeneous catalyst” preferably is a substance which is not soluble in water and/or is present in solid form.
• step (b) HMF reacts and di-HMF reacts, and a first portion of the resulting furane-2,5-dicarboxylic acid is a product of HMF and a second portion of the resulting furane-2,5-dicarboxylic acid is a product of di-HMF.
• the product mixture may also contain oxidation by-products.
• oxidation by-products which can be formed under oxidation conditions in step (b) of the process of the present invention, are 2,5-diformylfuran (DFF), 5-hydroxymethylfuran-2-carboxylic acid (HMFCA), 5-formylfuran-2-carboxylic acid (FFCA).
• oxygen-containing gas is a gas comprising gaseous compounds having one or more oxygen atoms per molecule.
• a preferred gaseous compound having one or more oxygen atoms per molecule is molecular oxygen (O 2 ).
• Air is a preferred oxygen-containing gas.
• oxidation conditions indicates conditions suitable for causing both HMF and di-HMF to react and to give furane-2,5-dicarboxylic acid in said product mixture also comprising water.
• the oxygen-containing gas acts as an oxidizing agent.
• reaction vessels can be used in step (b) to conduct the reaction of both HMF and di-HMF to furan-2,5-dicarboxylic acid (FDCA).
• FDCA furan-2,5-dicarboxylic acid
• an autoclave is used to conduct the reaction of HMF an di-HMF to FDCA.
• the reaction of HMF and di-HMF to FDCA is conducted in a batch reactor or in a semi-batch reactor. In other cases a plug flow or a fixed bed reactor is used.
• the reaction of two HMF molecules to one dimeric molecule results in a high content of by-products and therefore in a low yield of FDCA.
• the process according to the present invention converts both HMF and di-HMF into valuable FDCA, and thus the overall yield of the industrially important production of FDCA from hexoses is increased.
• a heterogeneous catalyst is used in the process of the present invention, thus allowing for a simplified work-up and other treatments of the product mixture and its ingredients.
• HMF and di-HMF are highly soluble in water thus increasing the maximum achievable starting concentration of HMF and di-HMF and therewith optimizing the space-time-yield of FDCA.
• water is relatively inert under the oxidation conditions of the present invention as it cannot be oxidized as easily as other solvents (e.g. acetic acid).
• the oxygen-containing gas employed as oxidizing agent is used in a more efficient way.
• the increasing concentration of protons in the reaction mixture catalyzes the hydrolytic cleavage of di-HMF into two HMF molecules thus increasing the concentration of HMF.
• the HMF formed by cleaving di-HMF is subsequently quickly converted into FDCA thereby further decreasing the pH and increasing the rate of the cleaving reaction.
• This allows to produce FDCA from di-HMF in an economically valuable time frame with no need of additional agents as used according to the prior art, for example HBr (see example 46 and 47 in WO 2013/033081) or similarly corrosive agents.
• the concentration of HMF should be sufficiently high to initiate the conversion of di-HMF to FDCA (in contrast to WO2013/033081).
• the deliberate presence of HMF for the acceleration of a process for preparing FDCA from di-HMF is therefore a primary reason for the advantages provided by the present invention.
• the oxidation of HMF and di-HMF into FDCA is conducted in a starting mixture comprising water.
• the total amount by weight of di-HMF preferably resulting from a previous process step (e.g. process step (a2) as described hereinbelow
• HMF is higher than the total amount of other organic compounds.
• the starting mixture used in the process according to the invention in step a) may comprise a comparatively high total concentration of reactant compound(s), HMF and di-HMF. This regularly leads to precipitation of FDCA during the catalytic conversion in step (b) and hence to the product mixture comprising FDCA in solid or dissolved form and the heterogeneous catalyst in solid form.
• both the heterogeneous catalyst and FDCA can be present in solid form.
• the heterogeneous catalyst is present in solid form and FDCA is present in its dissolved form.
• a heterogeneous catalyst used in step (b) may be part of a mixture of two, three or more than three heterogeneous catalysts.
• the product mixture formed in step (b) of a process according to the invention at least comprises water and a heterogeneous catalyst in separate phases, but many times comprises as a further solid phase the product FDCA.
• the proportion of the dissolved FDCA in the aqueous phase is typically low, because of the low solubility product of FDCA in water or aqueous solutions.
• the aqueous phase of the product mixture produced in step (b) of the present invention is a saturated solution with respect to FDCA.
• the product mixture obtained in step (b) can be optionally subjected to further treatment conditions resulting in a second product mixture.
• WO 2013/191944 A1 discloses that, under pressure and at a temperature in the range of 120° C. to 240° C., FDCA in solid form is dissolved in an appropriate aqueous solvent.
• an overheated aqueous solution may comprise a total proportion of dissolved FDCA in the range of from 10 to 20% by weight, based on the total amount of the aqueous solution.
• a subsequent (further treatment) step comprises heating the heterogeneous catalyst as present at the end of step (b) or as present at the end of an intermediate step following step (b) so that the activity of the heterogeneous catalyst after heating (i.e. its capability to act as a catalyst for the oxidation of HMF to FDCA) is increased in comparison with the heterogeneous catalyst as present at the end of step (b).
• the process of the present invention comprises a subsequent (further treatment) step as described above comprising heating the heterogeneous catalyst as present at the end of step (b) or as present at the end of an intermediate step following step (b) so that the activity of the heterogeneous catalyst after heating (i.e. its capability to act as a catalyst for the oxidation of HMF to FDCA) is increased, wherein the activity of the heterogeneous catalyst after the heating is increased by at least 5%, preferably by at least 10%, more preferably by at least 20%, even more preferably by at least 30%, most preferably by at least 50% in comparison with the activity of the heterogeneous catalyst as present at the end of step (b).
• a subsequent (further treatment) step as described above comprising heating the heterogeneous catalyst as present at the end of step (b) or as present at the end of an intermediate step following step (b) so that the activity of the heterogeneous catalyst after heating (i.e. its capability to act as a catalyst for the oxidation of HMF
• a process of the invention is preferred wherein the product mixture resulting in process step (b) is subjected to additional separation, purification and/or to (re-)crystallization steps to obtain purified FDCA.
• the starting mixture has a molar ratio of HMF to di-HMF in the range of from 100 to 0.8, preferably in the range of from 100 to 0.9
• the total weight of HMF and di-HMF in the starting mixture is in the range of from 0.1 to 50 wt.-%, preferably in the range of from 1 to 30 wt.-%, more preferably in the range of from 1 to 20 wt.-%, based on the total weight of the starting mixture.
• the starting mixture has a molar ratio of HMF to di-HMF in the range of from 100 to 20, in many other situations the range of from 10 to 0.9 is preferred.
• these ranges of molar ratios of HMF and di-HMF and/or this range of the total weight of HMF and di-HMF are preferred as those values represent optimum values for the production of FDCA from HMF or di-HMF.
• a relatively low amount of by-products is produced and the reaction can be conducted in an economically acceptable time frame.
• a concentration of over 50 wt.-% of HMF and di-HMF, based on the total starting mixture is in many cases disadvantageous, as the solubility characteristic of the reaction mixture is changed so that FDCA produced will likely precipitate, thus complicating post-synthetic work-up.
• a process of the invention is preferred, wherein the total amount of water in the starting mixture is at least 10 wt.-%, preferably at least 25 wt.-%, more preferably at least 50 wt.-%, based on the total weight of the starting mixture.
• the pH of the starting mixture is 4.0 or higher, preferably 4.5 or higher, more preferably 5.0 or higher, even more preferably 5.5 or higher, or the pH of the starting mixture is in the range of from 4.0 to 7.0, preferably the pH of the starting mixture is in the range of from 4.5 to 7.0, more preferably the pH of the starting mixture is in the range of from 5.0 to 7.0, even more preferably the pH of the starting mixture is in the range of from 5.5 to 7.0.
• the addition of solubilizers is optional.
• the starting mixture in step (b) does not comprise a solubilizer for FDCA.
• step (b) of the process of the present invention the development of the pH in the mixture subjected to oxidation conditions is not controlled by the addition of alkaline reagents.
• a process of the present invention is preferred, wherein the total amount of HMF in the starting mixture is in the range of from 0.1 to 40 wt.-%, preferably in the range of from 1 to 30 wt.-%, based on the total weight of the starting mixture.
• FDCA produced from initially present HMF accelerates the hydrolytic cleavage of di-HMF and thus accelerates the overall reaction. Therefore, concentrations of HMF in the starting mixture below 0.1 are not advantageous. On the other hand is a concentration of over 40 wt.-% of HMF, based on the total amount of the starting mixture, disadvantageous as the solubility characteristic of the reaction mixture is changed so that FDCA produced will likely precipitate.
• a process of the invention is preferred, wherein the total amount of di-HMF in the starting mixture is in the range of from 0.1 to 40 wt.-%, preferably in the range of from 0.1 to 30 wt.-%, more preferably in the range of from 0.1 to 10 wt.-%, even more preferably in the range of from 0.2 to 6 wt.-%, based on the total weight of the starting mixture.
• a concentration of over 40 wt.-% of di-HMF, based on the total weight of the starting mixture, is disadvantageous as the solubility characteristic of the reaction mixture is changed so that the FDCA produced will likely precipitate.
• the pH of the reaction mixture can be monitored in order to correspondingly monitor the conversion to FDCA during the reaction process. It is preferred to have a product mixture with a pH below 7 (preferably below 4) which generally means that an economically valuable amount of HMF or di-HMF to FDCA was converted.
• a process of the invention is preferred, wherein said starting mixture at a temperature in the range of from 70° C. to 200° C., preferably in the range of from 80° C. to 180° C., more preferably in the range of from 90° C. to 170° C., even more preferably in the range of from 100° C. to 140° C., is subjected to said oxidation conditions in the presence of said oxygen-containing gas and said catalytically effective amount of a heterogeneous catalyst comprising one or more noble metals on a support, so that both HMF and di-HMF react to give furane-2,5-dicarboxylic acid in the product mixture also comprising water and oxidation by-products.
• a process is preferred as described above (or as preferably described above), wherein said starting mixture is subjected to said oxidation conditions in a pressurized reactor, wherein during said reaction of HMF and di-HMF to FDCA oxygen or an oxygen-containing gas is continuously (or optionally and less preferred discontinuously) fed into and simultaneously removed from said reactor
• the pressure at which the reaction is conducted depends on the headspace volume of the reactor used which has to accommodate at least the required stoichiometric amount of oxygen-containing gas to fully convert the reactants HMF and di-HMF.
• a high pressure (of, for example, 20 or, for example, even 100 bar) is required in cases, where no continuous or discontinuously feed of an oxygen-containing gas is used, e.g. in a case where the reactor is once pressurized with an at least stoichiometric amount of an oxygen-containing gas at the beginning of the reaction without further manipulation of the pressure in the reactor.
• oxygen-containing gas is continuously or discontinuously replaced by fresh oxygen-containing gas.
• an oxygen partial pressure in the range of from 200 mbar and 10 bar is preferred.
• a process of the present invention is preferred, wherein said starting mixture is subjected to said oxidation conditions in a pressurized reactor, wherein the oxygen partial pressure in the reactor at least temporarily is in the range of from 100 mbar to 20 bar, preferably in the range of from 200 mbar to 10 bar, during the reaction of both HMF and di-HMF to furane-2,5-dicarboxylic acid.
• the oxidation is conducted at a pressure of 1 to 100 bar, preferably at a pressure of 1 to 20 bar in an atmosphere of an oxygen-containing gas or a mixture of an oxygen-containing gas and another gas (which is preferably inert under the reaction conditions).
• a process of the invention is preferred wherein said starting mixture does not comprise a catalytically effective amount of a homogeneous oxidation catalyst selected from the group of cobalt, manganese, and bromide compounds, and mixtures thereof.
• a homogeneous oxidation catalyst selected from the group of cobalt, manganese, and bromide compounds, and mixtures thereof.
• a process of the invention is preferred wherein the total amount of cobalt and manganese and bromide ions in the starting mixture is below 100 ppm, preferably below 20 ppm.
• a process of the invention is preferred wherein the total amount of carboxylic acid ions and carboxylic acid in the starting mixture is below 10 wt.-%, preferably below 5 wt.-%.
• the presence of a specific carboxylic acid or of its anions modifies the pH of the reaction mixture and therefore complicates the monitoring of the progress of the FDCA forming reactions by pH.
• This effect is even more pronounced as the carboxylic acids present can be oxidized by an oxygen-containing gas under the oxidation conditions of step (b) as described above to compounds with changed acidity, and this may effect the pH further. In such a case the pH could no longer be used as a measure for the progress of the FDCA forming reactions.
• a process of the present invention is preferred, wherein the total amount of acetate ions and acetic acid in said starting mixture is below 10 wt.-%, preferably below 1 wt.-%.
• step (a)) comprises
• acidic solvent designates an aqueous solvent mixture having a pH below 6 and/or a solvent (aqueous or non-aqueous) comprising a substance having a pKa below 5.
• process step (a2) as defined above
• process step (a2) often comprises a depolymerization and/or a dehydration step as described above. All aspects of a depolymerization and/or a dehydration step discussed herein above in the context of a process of preparing a starting mixture for a process for preparing furane-2,5-dicarboxylic acid apply mutatis mutandis for a process according to the present invention.
• step (a2) it is advantageous to conduct depolymerization and dehydration step (step (a2) as defined above) by using the same catalyst and/or the same reaction mixture and/or the same reactor.
• a step of preparing said starting mixture is preferred as described above (or as preferably described above) wherein process step (a3) is omitted (no additional treatment conditions are needed, e.g. solvent change) and the mixture resulting in process step (a2) is the starting mixture prepared in process step (a) and subjected to oxidation conditions of process step (b).
• step (a2) it is advantageous to conduct depolymerization and dehydration step (step (a2)), and the oxidation of HMF and di-HMF to FDCA (step (b)) in the same reactor.
• di-HMF is produced as a by-product during the conversion of hexoses or oligosaccharides or polysaccharides (e.g. cellulose) to HMF. It is therefore a further achievement of the present invention that di-HMF like HMF is converted to FDCA and thus contributes to an increase of the overall yield of the process.
• the addition of acidic solvent and/or carboxylic acid should be avoided in order to allow for a monitoring of the process of the reaction by measuring the pH.
• Another advantage of the process of the present invention as described above is the use of water as a solvent.
• a process of the invention is preferred, wherein in said heterogeneous catalyst comprising one or more noble metals on a support
• a process of the invention is particularly preferred, wherein in said heterogeneous catalyst comprising one or more noble metals on a support
• At least one of said noble metals is selected from the group consisting of platinum, iridium, palladium, osmium, rhodium and ruthenium, preferably platinum,
• said support is carbon
• Carbon is a suitable support for immobilizing noble metals as described above, in particular platinum, as it does not negatively influence the reaction kinetics of the conversion of HMF and di-HMF into FDCA.
• a process of the invention is preferred, wherein in said heterogeneous catalyst comprising one or more noble metals on a support
• the loading of platinum on the support should be at least 0.1 wt.-% (preferably at least 1 wt.-%), based on the total weight of heterogeneous catalysts comprising one or more noble metals on a support.
• a process of the invention is preferred, wherein in said heterogeneous catalyst comprising one or more noble metals on a support the molar ratio of said one or one of said more noble metals to the total amount of HMF and di-HMF is in the range of from 1:1 000 000 to 1:10, preferably in the range of from 1:10 000 to 1:10, more preferably in the range of from 1:1 000 to 1:100, preferably said one or one of said more noble metals is platinum.
• a process of the present invention is preferred, wherein the process is not a process comprising all of the following steps:
• a process of the invention is preferred wherein the product mixture obtained in step (b) comprises FDCA in dissolved form, and wherein the product mixture obtained in step (b) preferably does not comprise FDCA in solid form.
• the precipitation of FDCA in the presence of a heterogeneous catalyst is highly disadvantageous, as the effect of the precipitation of FDCA is that both heterogeneous catalyst and FDCA are present in solid form and can no longer be separated from one another in a simple manner.
• precipitation of FDCA leads, incidentally, to deactivation of the heterogeneous catalyst.
• the precipitation of FDCA on the internal and/or external catalyst surface of a heterogeneous catalyst can lead to contamination and possible deactivation of the heterogeneous catalyst. This involves coverage or coating of the catalytically active constituents of the heterogeneous catalyst by the precipitated FDCA, such that the catalytic constituents no longer come into contact with the reactants.
• the effect of such a contamination of the catalyst is that the catalyst does not display the same initial activity, if at all, and has to be replaced by new catalyst material which increases the costs. Especially in the case of utilization of costly catalysts, for example platinum catalysts, such a course of action is frequently uneconomic.
• the present invention also relates to the use of a catalyst comprising one or more noble metals on a support as an heterogeneous oxidation catalyst for accelerating in an aqueous starting mixture the conversion of both HMF and di-HMF to furane-2,5-dicarboxylic acid.
• the catalyst preferably is a catalyst as defined hereinabove or in the attached claims.
• Preferred is the use of a catalyst comprising one or more noble metals (preferably gold, platinum, iridium, palladium, osmium, silver, rhodium and ruthenium) on a support (preferably carbon, metal oxides, metal halides, and metal carbides).
• a catalyst comprising one or more noble metals on a support as an heterogeneous oxidation catalyst allows to conduct steps (a1), (a2), optionally (a3), and (b) without solvent exchange and without addition of expensive chemicals like acetic acid.
• a catalyst according to the present invention in processes as described above, in particular in processes of making FDCA. All aspects of or associated with processes of the invention as described above (or as preferably described above) can also be conducted by or in combination with the use of a catalyst according to the invention.
• the use according to the invention of a catalyst is preferred, wherein the pH of the starting mixture is 4.0 or higher, preferably 4.5 or higher, more preferably the pH of the starting mixture is in the range of from 4.0 to 7.0, most preferably the pH of the starting mixture is in the range of from 4.5 to 7.0.
• the pH of the starting mixture is 4.0 or higher, preferably 4.5 or higher, more preferably the pH of the starting mixture is in the range of from 4.0 to 7.0, most preferably the pH of the starting mixture is in the range of from 4.5 to 7.0.
• the starting mixture has a molar ratio of HMF to di-HMF in the range of from 100 to 0.8, preferably in the range of from 100 to 0.9,
• the total weight of HMF and di-HMF in the starting mixture is in the range of from 0.1 to 50 wt.-%, preferably in the range of from 1 to 30 wt.-%, more preferably in the range of from 1 to 10 wt.-%, based on the total weight of the starting mixture.
• the total amount of water in the starting mixture is at least 10 wt.-%, preferably at least 25 wt.-%, more preferably at least 50 wt.-%, based on the total weight of the starting mixture.
• the pH of the starting mixture is 4.0 or higher, preferably 4.5 or higher, more preferably 5.0 or higher, even more preferably 5.5 or higher, or the pH of the starting mixture is in the range of from 4.0 to 7.0, preferably the pH of the starting mixture is in the range of from 4.5 to 7.0, more preferably the pH of the starting mixture is in the range of from 5.0 to 7.0, even more preferably the pH of the starting mixture is in the range of from 5.5 to 7.0.
• the total amount of HMF in the starting mixture is in the range of from 0.1 to 40 wt.-%, preferably in the range of from 1 to 30 wt.-%, based on the total weight of the starting mixture.
• the total amount of di-HMF in the starting mixture is in the range of from 0.1 to 40 wt.-%, preferably in the range of from 0.1 to 30 wt.-%, more preferably in the range of from 0.1 to 10 wt.-%, even more preferably in the range of from 0.2 to 6 wt.-%, based on the total weight of the starting to mixture.
• said starting mixture at a temperature in the range of from 70° C. to 200° C., preferably in the range of from 80° C. to 180° C., more preferably in the range of from 90° C. to 170° C., even more preferably in the range of from 100° C. to 140° C. is subjected to said oxidation conditions in the presence of said oxygen-containing gas and said catalytically effective amount of a heterogeneous catalyst comprising one or more noble metals on a support, so that both HMF and di-HMF react to give furane-2,5-dicarboxylic acid in the product mixture also comprising water and oxidation by-products.
• said starting mixture does not comprise a catalytically effective amount of a homogeneous oxidation catalyst selected from the group of cobalt, manganese, and bromide compounds, and mixtures thereof.
• a homogeneous oxidation catalyst selected from the group of cobalt, manganese, and bromide compounds, and mixtures thereof.
• step of preparing said starting mixture comprises
• At least one of said noble metals is selected from the group consisting of platinum, iridium, palladium, osmium, rhodium and ruthenium, preferably platinum
• said support is carbon
• the molar ratio of said one or one of said more noble metals to the total amount of HMF and di-HMF is in the range of from 1:1 000 000 to 1:10, preferably in the range of from 1:10 000 to 1:10, more preferably in the range of from 1:1 000 to 1:100, preferably said one or one of said more noble metals is platinum.
• step (b) comprises furan-2,5-di carboxylic acid in dissolved form and wherein the product mixture obtained in step (b) preferably does not comprise furan-2,5-dicarboxylic acid in solid form.
• a catalyst comprising one or more noble metals on a support as an heterogeneous oxidation catalyst for accelerating in an aqueous starting mixture the conversion of both HMF and di-HMF to furane-2,5-dicarboxylic acid, wherein the catalyst preferably is a catalyst as defined in any of aspects 1 to 21.
• aqueous starting material mixture was prepared having a composition similar to the composition of HMF feed-streams usually obtained in sugar dehydration).
• D 2 O deuterated water
• HMF 99.9 atom %
• di-HMF 99+%
• the starting concentration C 0[HMF+di-HMF] of HMF+di-HMF in each aqueous reactant mixture was correspondingly 5% by weight, based on the total mass of the aqueous reactant mixture (total mass of deuterated water, HMF and di-HMF).
• the solid heterogeneous catalyst (0.928 g of 5 wt % Pt/C, 50 wt % H 2 O) was added to the respective aqueous reactant mixture and, thus, a reaction mixture comprising deuterated water, HMF, di-HMF, and the heterogeneous catalyst was obtained.
• the filled reactor was tightly sealed and pressurized with synthetic air (total pressure 100 bar to obtain conditions so that both HMF and di-HMF react to give FDCA.
• the starting mixture in the reactor comprising HMF, di-HMF and deuterated water was heated to a temperature of 100° C. while stirring at 2000 rpm. After reaching 100° C., this temperature was maintained for 18 hours while continuing stirring the heated and pressurized reaction mixture during the reaction time.
• a product mixture comprising FDCA, oxidation by-products, deuterated water and the heterogeneous catalyst resulted.
• the product mixture obtained was in the form of a suspension.
• a solution of deuterated sodium hydroxide (NaOD, 40 wt.-% in D 2 O, 99.5 atom % D, Sigma Aldrich) was carefully added to the product mixture until a slightly alkaline product mixture having a pH in the range of from 9 to 10 was reached.
• the slightly alkaline product mixture comprised the disodium salt of FDCA in completely dissolved form, and the heterogeneous catalyst in solid form.
• the heterogeneous catalyst in the slightly alkaline product mixture was separated from the solution by syringe filtration, and the filtrate (i.e. the remaining solution comprising the disodium salt of FDCA in completely dissolved form) was subsequently analyzed by 1 H-NMR spectroscopy.
• 1 H-NMR spectroscopy was used to determine the concentration of FDCA, FFCA, HMF and di-HMF.
• NMR-spectra were recorded in D 2 O at 299 K using a Bruker-DRX 500 spectrometer with a 5 mm DUL 13-1H/19F Z-GRD Z564401/11 probe, measuring frequency 499.87 MHz. Recorded Data were processed with the software Topspin 2.1, Patchlevel 6 (Supplier: Bruker BioSpin GmbH, Silberst Shape 4, 76287 Rheinstetten, Germany).
• Disodium salt of FDCA (disodium salt of compound of formula (I)):
• C [HMF] is the concentration in % by weight measured in the slightly alkaline product mixture and C 0[HMF] is the concentrations in % by weight measured based on the added amount of HMF and the volume of the starting mixture.
• Conversion [mol %] and “yield [mol %]” are average values calculated from a first value based on internal standard 1 and a second value based on internal standard 2 (general deviation is less than 5%).
• Y FDCA n FDCA n HMF + 2 ⁇ n di ⁇ - ⁇ HMF
• C [FDCA] is the concentration of FDCA in % by weight in the filtrate obtained in the fourth step
• C 0[HMF] is the HMF starting concentration in % by weight
• C 0[di-HMF] is the di-HMF starting concentration in % by weight
• M FDCA , M HMF and M di-HMF are the respective molecular weights in g/mol.
• table 1 shows that the yield of FDCA is increasing with increasing ratio n HMF /(h HMF +2n di-HMF ).

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