METHOD FOR PRODUCING OXIDE USING BETA-MANGANESE DIOXIDE

Abstract

With the object of efficiently producing an oxidation product, the present invention provides a method for producing an oxidation product by oxidizing a raw material compound in the presence of oxygen, wherein the raw material compound is oxidized in the presence of manganese dioxide having a crystal structure of β-type.

Claims

1-13. (canceled)

14. A method for producing an oxidation product by oxidizing a raw material compound in the presence of oxygen, wherein the raw material compound is oxidized in the presence of manganese dioxide having a crystal structure of β-type.

15. The method for producing an oxidation product according to claim 14, wherein the oxidation of the raw material compound is carried out in a liquid phase.

16. The method for producing an oxidation product according to claim 14, wherein a specific surface area of the manganese dioxide is 50 m.sup.2g.sup.−1 or more.

17. The method for producing an oxidation product according to claim 16, wherein the manganese dioxide is manganese dioxide produced by a method comprising the following steps: (1) mixing sodium permanganate and a strong acid salt of manganese(II) ion in water and stirring them; (2) collecting a precipitate after the step (1); and (3) calcining the precipitate collected in the step (2).

18. The method for producing an oxidation product according to claim 16, wherein the manganese dioxide is manganese dioxide produced by a method comprising the following steps: (1) mixing sodium permanganate and a weak acid salt of manganese(II) ion in water, then adding a strong acid, and thereafter stirring them; (2) collecting a precipitate after the step (1); and (3) calcining the precipitate collected in the step (2).

19. The method for producing an oxidation product according to claim 14, wherein the raw material compound is an organic substance.

20. The method for producing an oxidation product according to claim 14, wherein the raw material compound is 5-hydroxymethylfurfural, and the oxidation product is 2,5-furandicarboxylic acid.

21. A catalyst for oxidation reaction, comprising manganese dioxide having a crystal structure of β-type.

22. The catalyst for oxidation reaction according to claim 21, wherein a specific surface area of the manganese dioxide is 50 m.sup.2g.sup.−1 or more.

23. The catalyst for oxidation reaction according to claim 22, wherein the manganese dioxide is manganese dioxide produced by a method comprising the following steps: (1) mixing sodium permanganate and a strong acid salt of manganese(II) ion in water and stirring them; (2) collecting a precipitate after the step (1); and (3) calcining the precipitate collected in the step (2).

24. The catalyst for oxidation reaction according to claim 22, wherein the manganese dioxide is manganese dioxide produced by a method comprising the following steps: (1) mixing sodium permanganate and a weak acid salt of manganese(II) ion in water, then adding a strong acid, and thereafter stirring them; (2) collecting a precipitate after the step (1); and (3) calcining the precipitate collected in the step (2).

25. A method for producing manganese dioxide, comprising the following steps: (1) mixing sodium permanganate and a strong acid salt of manganese(II) ion in water and stirring them; (2) collecting a precipitate after the step (1); and (3) calcining the precipitate collected in the step (2), wherein a specific surface area of the manganese dioxide is 50 m.sup.2g.sup.−1 or more.

26. A method for producing manganese dioxide, comprising the following steps: (1) mixing sodium permanganate and a weak acid salt of manganese(II) ion in water, then adding a strong acid, and thereafter stirring them; (2) collecting a precipitate after the step (1); and (3) calcining the precipitate collected in the step (2), wherein a specific surface area of the manganese dioxide is 50 m.sup.2g.sup.−1 or more.

Description

BRIEF DESCRIPTION OF DRAWINGS

[0035] FIG. 1 shows scanning electron microscopic images of MnO.sub.2 synthesized. (a) α-MnO.sub.2, (b) β-MnO.sub.2, (c) γ-MnO.sub.2, (d) δ-MnO.sub.2, (e) ε-MnO.sub.2, (f) λ-MnO.sub.2

[0036] FIG. 2 is a view showing a pathway of oxidation reaction of HMF to FDCA. In the view, rate constants of aerobic oxidation of HMF using activated MnO.sub.2 are also shown.

[0037] FIG. 3 is a view showing results of analyses of MnO.sub.2 based on H.sub.2-TPR. (a) α-MnO.sub.2, (b) β-MnO.sub.2, (c) γ-MnO.sub.2, (d) δ-MnO.sub.2, (e) ε-MnO.sub.2, (f) λ-MnO.sub.2

[0038] FIG. 4 is a view showing a relationship between a 5-formyl-2-furancarboxylic acid (FFCA) oxidation rate (R.sub.0) and a reduction rate estimated from H.sub.2-TPR (.square-solid.: α-MnO.sub.2, .box-tangle-solidup.: β-MnO.sub.2, .circle-solid.: γ-MnO.sub.2, □: δ-MnO.sub.2, .diamond-solid.: ε-MnO.sub.2, Δ: λ—MnO.sub.2).

[0039] FIG. 5(a) shows XRD patterns of β-MnO.sub.2-HS-1 (upper side) and β-MnO.sub.2 (lower side, JCPDS 00-024-0735), and FIG. 5(b) shows a scanning electron microscopic image of β-MnO.sub.2-HS-1.

[0040] FIG. 6 is a view showing comparison between catalytic activity of β-MnO.sub.2 and that of β-MnO.sub.2-HS-1 for the oxidation reaction of HMF to FDCA.

DESCRIPTION OF EMBODIMENTS

[0041] Hereinafter, the present invention will be described in detail.

(A) Method for Producing Oxidation Product

[0042] The method for producing an oxidation product of the present invention is a method for producing an oxidation product by oxidizing a raw material compound in the presence of oxygen, and is characterized in that the raw material compound is oxidized in the presence of manganese dioxide having a crystal structure of β-type.

[0043] The manganese dioxide is not particularly limited as long as it has a crystal structure of β-type. Whether the crystal structure is β-type or not can be judged from the X-ray diffraction pattern. Manganese dioxide having a crystal structure of β-type can be produced in accordance with a known method (e.g., hydrothermal method or sol-gel method), but it is preferably produced by a method for producing high surface area manganese dioxide described later. The reason is that the manganese dioxide produced by this method has a high specific surface area and exhibits high catalytic activity. The “high specific surface area” referred to herein usually means 50 m.sup.2 g.sup.−1 or more, preferably means 60 m.sup.2g.sup.−1 or more, and more preferably means 70 m.sup.2g.sup.−1 or more. Although the upper limit of the specific surface area does not particularly exist, but it is usually 200 m.sup.2g.sup.−1 or less.

[0044] The raw material compound and the oxidation product produced are not limited to specific compounds (e.g., HMF and FDCA), and they may be any compounds as long as the compounds are a raw material compound and an oxidation product in the reaction on which manganese dioxide acts as a catalyst. The raw material compound is usually an organic substance but may be an inorganic substance. Specific examples of combinations of the raw material compound and the oxidation product produced include not only HMF and FDCA but also alcohols and aldehydes/ketones, amines and imines/nitriles, sulfides and sulfoxides, and thiols and sulfonamides, and more specific examples thereof include benzyl alcohol and benzaldehyde, 1-phenylethanol and acetophenone, benzylamine and benzonitrile, thioanisole and methyl phenyl sulfoxide, and benzenethiol and benzenesulfonamide.

[0045] As oxygen, pure oxygen may be used, or a gas containing oxygen (e.g., air) may be used.

[0046] The method for producing an oxidation product of the present invention is usually utilized for producing a useful compound such as FDCA, but can also be utilized for, for example, removal of a harmful substance, such as a deodorization method. In this case, the raw material compound is a harmful substance such as an odorant, and the oxidation product produced is not particularly a useful compound.

[0047] In the method for producing an oxidation product of the present invention, the oxidation is usually carried out in a liquid phase, particularly in an aqueous phase, but can also be carried out in a gas phase.

[0048] In the method for producing an oxidation product of the present invention, the raw material compound is oxidized in the presence of oxygen and manganese dioxide, and in the oxidation reaction of the raw material compound, substances other than oxygen and manganese dioxide may be present. For example, when the reaction is carried out in a liquid phase, the oxidation reaction is carried out in the presence of a solvent (water, organic solvent, or mixed solvent of water and organic solvent). The oxidation reaction is usually carried out in the presence of a base. Examples of the bases include NaHCO.sub.3, KHCO.sub.3, Na.sub.2CO.sub.3, K.sub.2CO.sub.3, NaOH, KOH and K.sub.3PO.sub.4. Among these, weak bases are preferably used, and NaHCO.sub.3 is particularly preferably used.

[0049] The amount of the manganese dioxide used is appropriately set according to the type of the raw material compound, etc. When the raw material compound is HMF, the amount of the manganese dioxide is usually 0.05 to 1.0 g, and preferably 0.1 to 0.5 g, based on 1 mmol of HMF. When the raw material compound is any of benzenethiols, the amount of the manganese dioxide is usually 0.02 to 0.5 g, and preferably 0.05 to 0.2 g, based on 1 mmol of the benzenethiol. When the raw material compound is any of benzyl alcohols, the amount thereof is usually 0.02 to 0.5 g, and preferably 0.05 to 0.2 g, based on 1 mmol of the benzyl alcohol.

[0050] The amount of the base used is appropriately set according to the types of the raw material compound and the base, etc. When the raw material compound is HMF and the base is NaHCO.sub.3, the amount of the base is usually 0.5 to 10 mmol, and preferably 2 to 3 mmol, based on 1 mmol of HMF.

[0051] The amount of the solvent used is appropriately set according to the type of the raw material compound, etc. When the raw material compound is HMF and the solvent is water, the amount of the solvent is usually 5 to 100 mL, and preferably 10 to 50 mL, based on 1 mmol of HMF. When the raw material compound is any of benzenethiols and the solvent is a mixed solvent of DMF and water, the amount of the solvent is usually 0.2 to 5.0 mL, and preferably 0.5 to 2 mL, based on 1 mmol of the benzenethiol. When the raw material compound is any of benzyl alcohols and the solvent is toluene, the amount of the solvent is usually 0.5 to 10.0 mL, and preferably 1.0 to 5.0 mL, based on 1 mmol of the benzyl alcohol.

[0052] The partial pressure of oxygen is appropriately set according to the type of the raw material compound, etc. When the raw material compound is HMF, the partial pressure of oxygen is usually 0.1 to 10 MPa, and preferably 0.5 to 5 MPa. When the raw material compound is any of benzenethiols, the partial pressure of oxygen is usually 0.1 to 10 MPa, and preferably 0.5 to 5 MPa. When the raw material compound is any of benzyl alcohols, it is usually 0.01 to 1 MPa, and preferably 0.05 to 0.5 MPa.

[0053] The temperature in the oxidation reaction is appropriately set according to the type of the raw material compound, etc. When the raw material compound is HMF, the temperature is usually 50 to 200° C., and preferably 80 to 120° C. When the raw material compound is any of benzenethiols, the temperature is usually 50 to 200° C., and preferably 70 to 110° C. When the raw material compound is any of benzyl alcohols, the temperature is usually 10 to 100° C., and preferably 30 to 80° C.

[0054] The reaction time is appropriately set according to the type of the raw material compound, etc. When the raw material compound is HMF, the reaction time is usually 6 to 48 hours, and preferably 12 to 36 hours. When the raw material compound is any of benzenethiols, the reaction time is usually 5 to 60 hours, and preferably 10 to 50 hours. When the raw material compound is any of benzyl alcohols, the reaction time is usually 6 to 48 hours, and preferably 12 to 36 hours.

[0055] After completion of the oxidation reaction, post treatment is carried out by a known method, as needed, and a desired oxidation product can be taken out. That is to say, after completion of the oxidation reaction, post-treatment operations such as filtration, washing, extraction pH adjustment, dehydration and concentration are carried out singly or in combination of two or more, as needed, and a desired oxidation product can be taken out by concentration, crystallization, reprecipitation, column chromatography or the like.

(B) Catalyst for Oxidation Reaction

[0056] The catalyst for oxidation reaction of the present invention is characterized by containing manganese dioxide having a crystal structure of β-type.

[0057] The catalyst for oxidation reaction of the present invention is usually composed of only manganese dioxide having a crystal structure of β-type, but may contain other substances.

[0058] The manganese dioxide used may be the same as the manganese dioxide used in the aforesaid method for producing an oxidation product of the present invention.

(C) Method for Producing High Surface Area Manganese Dioxide

(C-1) First Method for Producing High Surface Area Manganese Dioxide

[0059] The first method for producing manganese dioxide of the present invention is characterized by comprising the following steps (1) to (3). The manganese dioxide produced by this method has a crystal structure of β-type and has a high specific surface area. The manganese dioxide produced by this first method for producing manganese dioxide is sometimes referred to as “β-MnO.sub.2-HS-1”.

[0060] In the step (1), sodium permanganate and a strong acid salt of manganese(II) ion are mixed in water and stirred.

[0061] Examples of the strong acid salts of manganese(II) ion include manganese sulfate and manganese nitrate.

[0062] The amount of water used is not particularly limited, but it is usually 1 to 40 mL, and preferably 5 to 20 mL, based on 1 mmol of sodium permanganate.

[0063] The stirring time is not particularly limited either, but it is usually 1 to 40 min, and preferably 10 to 30 min.

[0064] Through this step, amorphous manganese dioxide is produced.

[0065] In the step (2), a precipitate is collected after the step (1).

[0066] The collection can be carried out by filtration or the like. The collected precipitate is usually washed with water or the like, subsequently dried and thereafter used in the next step.

[0067] In the step (3), the precipitate collected in the step (2) is calcined.

[0068] The calcining temperature is not particularly limited, but it can be set to, for example, 200 to 600° C.

[0069] The calcining time is not particularly limited either, but it can be set to, for example, 2 to 10 hours.

(C-2) Second Method for Producing High Surface Area Manganese Dioxide

[0070] The second method for producing manganese dioxide of the present invention is characterized by comprising the following steps (1) to (3). The manganese dioxide produced by this method also has a crystal structure of β-type and has a high specific surface area. The manganese dioxide produced by this second method for producing manganese dioxide is sometimes referred to as “β-MnO.sub.2-HS-2”.

[0071] In the step (1), sodium permanganate and a weak acid salt of manganese(II) ion are mixed in water, then a strong acid is added, and thereafter, they are stirred.

[0072] The weak acid salt of manganese(II) ion is, for example, manganese acetate. Examples of the strong acids include sulfuric acid and nitric acid.

[0073] The amount of water used is not particularly limited, but it is usually 1 to 40 mL, and preferably 5 to 20 mL, based on 1 mmol of sodium permanganate.

[0074] The amount of the strong acid added is not particularly limited, but the strong acid is usually added in such an amount that pH becomes 1.5 or less, and is preferably added in such an amount that pH becomes 0.8 or less.

[0075] The stirring time is not particularly limited either, but it is usually 1 to 120 min, and preferably 10 to 60 min.

[0076] Through this step, amorphous manganese dioxide is produced.

[0077] In the step (2), a precipitate is collected after the step (1).

[0078] The collection can be carried out by filtration or the like. The collected precipitate is usually washed with water or the like, subsequently dried and thereafter used in the next step.

[0079] In the step (3), the precipitate collected in the step (2) is calcined.

[0080] The calcining temperature is not particularly limited, but it can be set to, for example, 200 to 600° C.

[0081] The calcining time is not particularly limited either, but it can be set to, for example, 2 to 10 hours.

EXAMPLES

[0082] Hereinafter, the present invention will be described in more detail with reference to examples, but the present invention is in no way limited to these examples.

Example 1

(A) Experimental Method

(1) Experimental Instrument

[0083] On a diffractometer (Ultima IV, Rigaku; Cu K a, λ=1.5405 Å, 40 kV-40 mA) equipped with a high-speed one-dimensional detector (D/teX Ultra, Rigaku), an XRD pattern was recorded. The diffraction data were collected in the range of 2θ=10 to 80° at a scanning rate of 20° min.sup.−1 and a step of 0.02°. ICP-AES analysis was carried out by Shimadzu ICPS-8100 spectrometer. A nitrogen adsorption-desorption isotherm was measured at 77 K using a surface area analyzer (Nova-4200e, Quantachrome). Before the measurement, the sample was heated at 423 K for 1 hour under vacuum to remove physisorbed water. Brunauer-Emmett-Teller (BET) surface area was estimated over a relative pressure (P/PO) range of 0.05 to 0.30. The shape of the sample was examined using a scanning electron microscope (SEM; S-5500, Hitachi). TG-DTA measurement was carried out using a differential thermal analyzer (TG8120, Rigaku). TG-DTA analysis was carried out at a heating rate of 10 K min.sup.−1 from room temperature to 1273 K in a stream of N.sub.2 (200 mL min.sup.1) XPS analysis was carried out using Shimadzu ESCA-3400HSE spectrometer using Mg Kα radiation (1253.6 eV) at 10 kV and 25 mA. The sample was pressed to prepare pellets, and the pellets were fixed onto a double-sided carbon tape. The binding energy was calibrated using C is band of 284.6 eV. Using the XPS Peak 4.1 program, the spectrum was fitted and evaluated, but the background was subtracted using a Shirley function. The deconvoluted Mn 2p spectrum of MnO.sub.2 shows three peaks having binding energies of 640.8, 641.8, 642.8 and 644.5 eV corresponding to Mn.sup.II, Mn.sup.III, Mn.sup.IV and shake-up peak, respectively. Using Mettler Toledo Easy Pro Titrator System, iodine titration was carried out. About 10 mg of MnO.sub.2 was added to a mixture of a 0.5 M HCl aqueous solution (12 mL) and a 2 M KI aqueous solution (5 mL), and the resulting solution was titrated with a 0.01 M Na.sub.2S.sub.3O.sub.3 aqueous solution. H.sub.2TPR profile was measured by BEL Japan BELCAT-A chemisorption analyzer equipped with a thermal conductivity detector (TCD). In a quartz cell, 50 mg of a sample was placed, and subsequently, the sample was heated at a rate of 10 K min.sup.−1 from 323 K to 923 K in a stream of 5% H.sub.2/Ar (50 mL min.sup.−1). The initial reduction rate was estimated in a range of 553 K up to 593 K, this corresponded to a range of less than 10% of a lattice oxygen atom having been reduced by H.sub.2, and all the MnO.sub.2 catalysts were stable in this range. Using a photo diode array (PDA) and a refractive index (RI) detector, high performance liquid chromatography (HPLC; LC-2000, Jasco) analysis was carried out with Aminex HPX-87H column (7.8 mm diameter×300 mm, Bio-Rad Laboratories, Inc. Co. Ltd.; eluent (0.5 mM H.sub.2SO.sub.4), flow rate (0.5 mL/min), column temperature (308 K)). The retention times of FDCA, 5-hydroxymethyl-2-furancarboxylic acid (HMFCA), FFCA, HMF and 2,5-diformyl furan (DFF) were 20.9, 27.3, 29.4, 41.7, and 52.1 minutes, respectively. The crystal structure was drawn by utilizing visualization of the electronic and structural analysis (VESTA) program.

(2) Experimental Method for Oxidation Reaction

[0084] Oxidation reaction was carried out using a 30 mL capped test tube or an autoclave reaction vessel having a 13 mL Teflon (registered trademark) container. Typical oxidation reaction of HMF was carried out in accordance with the following procedure. Into the autoclave reaction vessel, HMF (0.2 mmol), MnO.sub.2 (0.05 g), NaHCO.sub.3 (0.6 mmol), pure water (5 mL) and O.sub.2 (1 MPa) were introduced, and they were allowed to react at 100° C. for 24 hours. After the reaction, the catalyst was separated by filtration, and the filtrate was diluted to 10 times with pure water and analyzed by HPLC. The collected catalyst was washed with pure water (25 mL), then dried at 80° C., and reused for the experiment.

(3) Synthesis of High Surface Area β-MnO.sub.2 (β-MnO.sub.2-HS-1)

[0085] β-MnO.sub.2-HS-1 was synthesized in accordance with the following procedure. To an aqueous solution (20 mL) of NaMnO.sub.4 (1.28 g, 4 mmol) having been vigorously stirred, an aqueous solution (20 mL) of MnSO.sub.4.5H.sub.2O (1.45 g, 6 mmol) was dropwise added, and after addition of all the solution, they were stirred for 10 minutes. A precipitate was collected by filtration, washed with pure water (300 mL), and then dried at 353 K overnight. The dried precipitate was calcined at 400° C. for 5 hours, whereby β-MnO.sub.2-HS-1 that was a black powder was obtained. Yield: 0.83 g (96%)

[0086] A surface area of the resulting β-MnO.sub.2-HS-1 was 73 m.sup.2g.sup.−1, and an average pore diameter thereof was 3.5 nm.

(4) Synthesis of β-MnO.SUB.2 .by Hydrothermal Method

[0087] β-MnO.sub.2 was synthesized in accordance with the procedure previously reported (Y. Y. Gorbanev, S. Kegnaes, A. Riisager, Top. Catal. 2011, 54, 1318-1324). In water (40 mL), NaMnO.sub.4 (1.28 g, 4 mmol) was dissolved, to the solution was added MnSO.sub.4.5H.sub.2O (2.89 g, 12 mmol) while stirring, and they were further stirred for 30 minutes. This mixture was transferred into a stainless steel autoclave equipped with a Teflon (registered trademark) inner cylinder type closed container (TAF-SR type, Taiatsu Techno Corporation). The mixture was heated at 433 K for 12 hours, and thereafter, a precipitate was collected, washed with water (300 mL) and dried at 353 K overnight, thereby obtaining a black powder of β-MnO.sub.2. Yield: 1.66 g (83%)

(B) Experimental Result

(1) Effect of MnO.SUB.2 .Crystal Structure on Oxidation Reaction of HMF to FDCA

[0088] Syntheses and characterizations of MnO.sub.2 having various crystal structures were carried out, and their oxidation catalytic action was studied. α-, β-, γ-, δ-, ε- and λ-MnO.sub.2 were synthesized. From XRD analysis of each sample, production of tetragonal crystal α-MnO.sub.2, tetragonal crystal β-MnO.sub.2, orthorhombic crystal γ-MnO.sub.2, trigonal crystal δ-MnO.sub.2, hexagonal crystal ε-MnO.sub.2, and cubic crystal λ-MnO.sub.2 was confirmed. Metal content, water content, and average oxidation state (AOS) of the Mn species were determined by ICP-AES, TG-DTA, and iodine reduction titration, respectively. The results are set forth in Table 1. The amount of Mn in every MnO.sub.2 catalyst was 47.86 to 62.39 wt %. The AOS of each of the β-, γ- and ε-MnO.sub.2 was about 4, while the AOS of each of the α-, δ- and λ-MnO.sub.2 was smaller (3.70 to 3.81) because of influence of charge compensation due to the presence of K.sup.+ ion.

[0089] Scanning electron microscopic (SEM) images of the synthesized MnO.sub.2 are shown in FIG. 1. The shapes and the average sizes are listed in Table 1. The α-, β- and γ-MnO.sub.2 were each composed of rod-like particles, and the particle diameter depended upon the sample. The δ- and λ-MnO.sub.2 were each composed of spherical particles, and the ε-MnO.sub.2 was composed of rose-like particles. Regarding the specific surface areas of MnO.sub.2 calculated from the BET plot of the N.sub.2 adsorption isotherm (77 K), the specific surface area of the ε-MnO.sub.2 (181 m.sup.2g.sup.−1) was considerably large, but the specific surface areas of the α-, β-, γ-, δ- and λ-MnO.sub.2 were of medium values to low values (14 to 67 m.sup.2g.sup.−1). These results were in good agreement with the average particle diameters obtained from the SEM observation.

TABLE-US-00001 TABLE 1 Sulk content, surface area, particle shape and particle size of MnO.sub.2 catalyst .sup.a Catalyst Bulk content (wt %) Specific surface area (m.sup.2g.sup.−1) Particle shape Particle size .sup.d (nm) α-MnO.sub.2 Mn: 56.75: K: 712; water: 0.82 30 rod-like .sup.a 30-60 wide 60-1000 long 50-70 wide β-MnO.sub.2 Mn. 60.81; water: 0.46 14 rod-like .sup.a 150-1000 long 10-60 wide γ-MnO.sub.2 Mn: 62.03; water: 2.45 39 rod-like .sup.a 40-800 long δ-MnO.sub.2 Mn: 52.43; K. 8.67; water: 35 spherical .sup.b 50-150 6.86 rose-like .sup.c 10-20 thick ε-MnO.sub.2 Mn: 47.86; Fe: 6.1; water: 4.84 181 (constituted of 60-200 wide nanoplates) λ-MnO.sub.2 Mn: 62.39; water: 3.76 67 spherical .sup.b 40-70 .sup.a The nano rod particle size means a diameter and a length. .sup.b average particle diameter, .sup.c thickness and length of nanoplate, .sup.d particle size based on SEM observation

[0090] Using the MnO.sub.2 catalysts having various crystal structures, oxidation reaction of HMF using O.sub.2 (1 MPa) as an oxidizing agent in the presence of NaHCO.sub.3 (3 equiv. based on HMF) was studied. The results are set forth in Table 2. In every case, the HMF conversion ratio was in the range of 93 to 99%. Among the catalysts studied, the activated MnO.sub.2, the α-MnO.sub.2 and the ε-MnO.sub.2 exhibited FDCA yields of 59 to 74%. On the other hand, the β-, γ-, δ- and λ-MnO.sub.2 exhibited high HMF conversion ratios, but as a main product, FFCA was produced in a ratio of 60 to 69%, and the FDCA yields were of low values (5 to 28%). In order to confirm stability of the MnO.sub.2 catalysts, XRD pattern of each catalyst after the reaction and the amount of a metal in the filtrate based on the ICP-AES analysis were measured. In all the catalysts except the ε-MnO.sub.2, elution of Mn species into the filtrate was not confirmed. There was almost no change in the positions of the XRD peaks of the α-, β- and ε-MnO.sub.2 between before and after the reaction, but the peak intensities of the α- and β-MnO.sub.2 slightly increased. In the γ-MnO.sub.2, peak shift accompanying the unit cell extension due to H insertion was confirmed. On the other hand, the XRD patterns of the δ- and λ-MnO.sub.2 greatly changed after the reaction. In the δ-MnO.sub.2, the intensities of (003) and (006) peaks assigned to layer structure greatly decreased, and elution of K.sup.+ ion of 55% into the filtrate was confirmed. Moreover, in the XRD pattern of the λ-MnO.sub.2 after the reaction, peaks having been observed before the reaction almost disappeared. These results have suggested that the structures of the δ- and λ-MnO.sub.2 are unstable under the present reaction conditions.

TABLE-US-00002 TABLE 2 Influence of MnO.sub.2 catalyst on oxidation of HMF to FDCA .sup.a [00001] [00002] Yieid (%) Catalyst Conversion ratio (%) HMFCA DFF FFCA FDCA Activated MnO.sub.2 >99 — — 15 74 α-MnO.sub.2 >99 1 0 36 59 β-MnO.sub.2 >99 1 — 66 28 γ-MnO.sub.2   93 2 3 60 5 δ-MnO.sub.2   96 — 1 69 10 ε-MnO.sub.2 >99 1 — 27 63 λ-MnO.sub.2 >99 — — 66 12 .sup.a Reaction conditions: catalyst (0.05 g), HMF (0.2 mmol), NaHCO.sub.3 (0.6 mmol), water (5 mL), pO.sub.2 (1 MPa), 373 K, 24 h.
(2) Reaction Mechanism in Oxidation Reaction of HMF to FDCA with Activated MnO.sub.2 Catalyst

[0091] Since the oxidation of HMF to FDCA is a complicated successive reaction, it is difficult to evaluate fundamental reactivity of the MnO.sub.2 catalyst. Then, determination of a key step in the HMF oxidation with the activated MnO.sub.2 catalyst was carried out by the kinetic analysis. FIG. 2 shows a reaction pathway from HMF to FDCA. By the oxidation of a hydroxyl group and a formyl group of HMF, DFF and HMFCA are given, respectively. By the successive oxidation of DFF and HMFCA, FFCA is obtained, and FFCA is finally oxidized into FDCA. The reaction pathway from HMF to FFCA depends upon the catalytic system, and the mechanism via HMFCA has been reported in an Au, Pt, Ru, or Pd supported catalyst/NaOH/O.sub.2 reaction system, while the mechanism via DFF and HMFCA has been reported in a Pt/C catalyst/NaHCO.sub.3/O.sub.2 reaction system.

[0092] Assuming that every step is a reaction of primary dependence on a substrate, rate constants (k.sub.1 to k.sub.5 in FIG. 2) are estimated from fitting to time changes, and in the activated MnO.sub.2 catalyst, the estimation resulted in k.sub.1=2.4×10.sup.−3, k.sub.2=2.0×10.sup.−4, k.sub.3=4.2×10.sup.−2, k.sub.4=1.2×10.sup.−3, and k.sub.5=4.6×10.sup.−4. k.sub.2 is about 10 times smaller than K.sub.1, and this suggests that the mechanism from HMF to FFCA is mechanism via DFF. This is also supported by oxidation of alcohol with MnO.sub.2 being generally faster than aldehyde oxidation. From the fact that the value of k.sub.5 is smaller than the values of k.sub.1, k.sub.3 and k.sub.4, it has been suggested that the oxidation reaction of FFCA to FDCA is a rate-determining step in the present reaction.

(3) Influence of MnO.SUB.2 .Crystal Structure on Oxidation of FFCA to FDCA

[0093] By comparing rates (R.sub.0) of oxidation reaction of FFCA to FDCA, the reaction being a rate-determining step of the oxidation reaction of HMF to FDCA, on the basis of the results of the kinetic analysis, a structure-reactivity correlation in the oxidation reaction with a MnO.sub.2 catalyst was studied (Table 3). The initial rate per surface area decreased in the order of β-MnO.sub.2 (16.4 μmol h.sup.−1 m.sup.−2)>λ-MnO.sub.2 (12.2 μmol h.sup.−1 m.sup.−2)>α-MnO.sub.2 (7.6 μmol h.sup.−1 m.sup.−2)>γ-MnO.sub.2 (7.4 μmol h.sup.−1 m.sup.−2)>δ-MnO.sub.2 (5.3 μmol m.sup.−2)>ε-MnO.sub.2 (2.3 μmol h.sup.−1 m.sup.−2).

TABLE-US-00003 TABLE 3 Influence of synthetic MnO.sub.2 catalyst on oxidation of FFCA to FDCA .sup.a [00003] [00004] Conversion FDCA Catalyst ratio (%) Yield (%) R.sub.0 (μ mol h.sup.−1 m.sup.−2) Activated MnO.sub.2 30 34 5.6 α-MnO.sub.2 8 12 7.6 β-MnO.sub.2 7 12 16.4 γ-MnO.sub.2 10 14 7.4 δ-MnO.sub.2 6 9 5.3 ε-MnO.sub.2 16 21 2.3 λ-MnO.sub.2 47 50 12.2 .sup.a Reaction conditions: catalyst (0.05 g), FFCA (0.2 mmol), NaHCO.sub.3 (0.6 mmol), water (5 mL), pO.sub.2 (1 MPa), 373 K, 2 h.

[0094] In order to confirm excellent FFCA oxidation capacity of the β-MnO.sub.2 among various MnO.sub.2, XPS measurement was carried out. Peak separation results of spectra of the MnO.sub.2 catalysts are set forth in Table 4. As surface species, Mn.sup.4+, Mn.sup.3+ and Mn.sup.2+ species were observed, and the surface Mn valences were estimated to be 3.00 to 3.57. The O is peak was separable into three peaks assigned to lattice oxygen, adsorbed oxygen and adsorbed water. It has been reported that the valence of a metal or the state of adsorbed oxygen species plays an important role in the oxidation reaction with a metal oxide catalyst, but a correlation between the reactivity and the surface Mn valence or the amount of adsorbed oxygen has not been confirmed. From these results, the reactivity cannot be explained only by the above two factors, and it is thought that a difference in fundamental reactivity of an oxygen atom accompanying the crystal structure plays an important role in the present oxidation reaction.

TABLE-US-00004 TABLE 4 Binding energy, fraction, and average oxidation state of synthetic MnO.sub.2 catalyst .sup.a Binding energy of Mn 2p (eV) Binding energy of O 1s (eV) Catalyst Mn (IV) Mn (III) Lattice oxygen Adsorbed oxygen Adsorbed water α-MnO.sub.2 642.36 (54%) 641.36 (46%) 529.5 (77%) 531.2 (19%) 533.0 (4%) β-MnO.sub.2 642.23 (44%) 641.23 (56%) 529.2 (74%) 531.2 (23%) 533.0 (3%) γ-MnO.sub.2 642.15 (54%) 641.15 (46%) 529.4 (71%) 531.2 (25%) 533.0 (4%) δ-MnO.sub.2 642.46 (36%) 641.46 (64%) 529.7 (73%) 531.4 (21%) 533.0 (6%) ε-MnO.sub.2.sup.b 642.44 (32%) 641.44 (38%) 529.5 (69%) 531.4 (27%) 533.0 (4%) λ-MnO.sub.2 642.17 (53%) 641.17 (47%) 529.6 (71%) 531.4 (25%) 533.0 (4%) .sup.a Each value in parentheses is a percentage of a peak. .sup.b Mn.sup.2+ species was observed on a surface of ε-MnO.sub.2.

[0095] The results of analyses of MnO.sub.2 based on the H.sub.2 temperature-programmed reduction method (H.sub.2-TPR) are shown in FIG. 3. Reduction of all the MnO.sub.2 catalysts started from temperatures of 410 to 470 K, and two main reduction peaks assigned to (i) reduction of MnO.sub.2 to Mn.sub.3O.sub.4 (via Mn.sub.2O.sub.3) and (ii) reduction of Mn.sub.3O.sub.4 to MnO were confirmed. The peak top temperature was different for each crystal phase, and a good correlation between the peak top temperature and the reactivity was not confirmed. It has been reported that owing to an increase in diffusion resistance due to a decrease in catalyst surface area, the reduction peak top temperature shifts to a higher temperature, and that the oxidation reaction rate is correlated with the initial reduction rate. Actually, the reactivity depended upon not the reduction peak top temperature but the initial reduction rate, and the reduction rate per surface area estimated from the H.sub.2-TPR decreased in the order of β-MnO.sub.2 (174 H.sub.2 μmol h.sup.−1 m.sup.−2)>δ-MnO.sub.2 (161 H.sub.2 μmol h.sup.−1 m.sup.−2)>λ-MnO.sub.2 (95 H.sub.2 μmol h.sup.−1 m.sup.−2)>α-MnO.sub.2 (89 H.sub.2 μmol h.sup.−1 m.sup.−2)>γ-MnO.sub.2 (69 H.sub.2 μmol h.sup.−1 m.sup.−2)>ε-MnO.sub.2 (23 H.sub.2 μmol h.sup.−1 m.sup.−2). A plot of the reduction rate against the reaction rate of the FFCA oxidation is shown in FIG. 4. Except for unstable δ- and λ-MnO.sub.2, an almost linear relationship was confirmed, and it is thought that the oxidation of a substrate supports mechanism of reaction that is promoted by an oxygen atom in MnO.sub.2.

[0096] Synthesis of β-MnO.sub.2 by hydrothermal method or sol-gel method has been reported, but their specific surface areas are generally low and restrict catalytic performance. The present inventor has developed a novel synthesis method for β-MnO.sub.2 and succeeded in improvement of a specific surface area up to 73 m.sup.2 g.sup.−1 from 14 m.sup.2g.sup.−1. By calcining an amorphous precursor obtained by mixing Na[MnO.sub.4] and Mn(SO.sub.4) in a molar ratio of 2:3, pure high surface area β-MnO.sub.2 (β-MnO.sub.2-HS-1) was obtained. The XRD pattern for the β-MnO.sub.2-HS-1 was in good agreement with that of tetragonal crystal β-MnO.sub.2 (FIG. 5(a)), and the SEM image showed a rose-like particle constituted of small nanoplates (FIG. 5(b)). When the β-MnO.sub.2-HS-1 was applied to FDCA synthesis due to HMF oxidation, the FDCA yield for 24 hours was 88% and was greatly improved as compared with that of β-MnO.sub.2 synthesized by hydrothermal method (FIG. 6).

Example 2

(1) Sulfonamide Synthesis Reaction

[0097] Oxidation reaction was carried out using an autoclave reaction vessel having a 13 mL Teflon (registered trademark) container. Typical sulfonamide synthesis reaction was carried out in accordance with the following procedure. Into the autoclave reaction vessel, benzenethiol (1.0 mmol), MnO.sub.2 (0.1 g), a 28% NH.sub.3 aqueous solution (5.0 mmol), DMF/H.sub.2O (0.6/0.4 mL), and O.sub.2 (1 MPa) were introduced, and they were allowed to react at 90° C. for 20 hours. After the reaction, the catalyst was separated by filtration, and isolation and collection of a product in the filtrate were carried out using an elution position control automated setup medium pressure preparative liquid chromatograph (EPCLC-AI-580S, manufactured by Yamazen Corporation).

[0098] The yields of benzenesulfonamides produced are set forth in the following table.

TABLE-US-00005 TABLE 5 Oxidative sulfonamidation of compound 1 to compound 2 using β-MnO.sub.2—HS-1 .sup.[a] en- yield.sup.[b] try substrate product (%) 1.sup.   [00005] [00006] 88% 1a 2a 2.sup.   [00007] [00008] 88% 1b 2b 3.sup.   [00009] [00010] 82% 1c 2c 4.sup.[c] [00011] [00012] 83% 1d 2d 5.sup.   [00013] [00014] 80% 1e 2e 6.sup.   [00015] [00016] 85% 1f 2f 7.sup.   [00017] [00018] 82% 1g 2g 8.sup.[d] [00019] [00020] 68% 1h 2h 9.sup.[e] [00021] [00022] 59% 1i 2i 10.sup.[c] [00023] [00024] 41% 1j 2j .sup.[a] Reaction conditions: β-MnO.sub.2—HS-1 (0.1 g), thiols (1 mmol), DMF/water (0.6/0.4 mL), 28% NH.sub.3 aqueous solution (5 mmol), ρO.sub.2 (1 MPa), 90° C., 20 hours .sup.[b]Isolated yield; In every reaction, the conversion ratio of the compound 1 became 99% or more. Yield (%) = product (mol)/initial substrate (mol) × 100 .sup.[c]The reaction time was set to 40 hours. .sup.[d]DMF (1 mL) was used. Instead of the NH.sub.3 aqueous solution, NH.sub.3 gas (0.5 MPa) was used. .sup.[e]β-MnO.sub.2—HS-1 (0.15 g) was used.

(2) Oxidation Reaction of Alcohol

[0099] Oxidation reaction was carried out using a 30 mL capped test tube. Typical alcohol oxidation reaction was carried out in accordance with the following procedure. Into the test tube, benzyl alcohol (1.0 mmol), MnO.sub.2 (0.1 g), toluene (2 mL) and O.sub.2 (0.1 MPa) were introduced, and they were allowed to react at 50° C. for 24 hours. Qualification and quantification of the reaction products were carried out using a gas chromatograph.

TABLE-US-00006 TABLE 6 Oxidation of alcohol to aldehyde using β-MnO.sub.2—HS-1 .sup.[a] yield entry substrate product (%) 1 [00025] [00026]   98% 2 [00027] [00028]   94% 3 [00029] [00030] >99% .sup.[a] Reaction conditions: β-MnO.sub.2—HS-1 (0.1 g), alcohols (1 mmol), toluene (2 mL), ρO.sub.2 (0.1 MPa), 50° C., 24 hours; In every reaction, the conversion ratio of each alcohol became 99% or more. Yield (%) = product (mol)/initial substrate (mol) × 100
(3) Synthesis of High Surface Area β-MnO.sub.2 (β-MnO.sub.2-HS-2)

[0100] β-MnO.sub.2-HS-2 was synthesized in accordance with the following procedure. To an aqueous solution (20 mL) of NaMnO.sub.4.H.sub.2O (0.64 g, 4 mmol) having been vigorously stirred, an aqueous solution (20 mL) of Mn(OAc).sub.2.4H.sub.2O (1.47 g, 6 mmol) was dropwise added, and a 0.5 M H.sub.2SO.sub.4 aqueous solution was added to adjust pH to 0.74, following by stirring for 30 minutes. A precipitate was collected by filtration, washed with pure water (2 L), and then dried at 80° C. overnight. The dried precipitate was calcined at 400° C. for 5 hours, whereby β-MnO.sub.2-HS-2 that was a black powder was obtained. Yield: 0.8852 g (82%)

[0101] A surface area of the resulting β-MnO.sub.2-HS-2 was 129 m.sup.2g.sup.−1, and an average pore diameter thereof was 5 to 7 nm.

[0102] All the publications, the patents and the patent applications cited in the present specification are incorporated into the present specification as references, as they are.

INDUSTRIAL APPLICABILITY

[0103] Since the method for producing an oxidation product of the present invention can be used for producing useful substances such as FDCA, this method is applicable in industrial fields related to production of such substances.