KR102468423B1 - A catalyst for reforming of xylose comprising a metallic nanoparticle and the method for producing the same - Google Patents

Abstract

In this specification, the support; and metal particles dispersed on the support, wherein the metal particles have an average diameter of 0.6 to 2.2 nm.

Description

Catalyst for xylose reforming reaction containing metal nanoparticles and method for producing the same

The present invention discloses a catalyst for xylose reforming reaction containing metal nanoparticles and a method for preparing the same.

Hydrogen is a major source of fuel cells today, mainly produced through steam reforming of natural gas or coal gasification to produce carbon dioxide. Therefore, many studies have recently been conducted on the development of hydrogen production technologies using clean energy sources such as water and biomass. In particular, the method of producing hydrogen from biomass or biomass-derived chemicals, in addition to the method via electrolysis of water, is possible because the carbon dioxide produced during biomass reforming/gasification can be recycled through photosynthesis providing a closed carbon loop. Carbon neutrality has received considerable attention as a possible transformation method. Moreover, biomass represents a naturally abundant and superior next-generation energy source compared to fossil fuels, which are rapidly depleting worldwide.

As a technology for producing hydrogen from biomass, a method using a pyrolysis reaction, a gasification reaction, and a biological process has been developed so far. In addition, methods for producing hydrogen from aqueous phase reforming (APR) using biomass-based chemicals have been comprehensively studied. Since this method has thermodynamically favorable reaction conditions compared to the general water-gas shift reaction (WGS), high hydrogen yield can be obtained with a small amount of carbon monoxide in APR. Also, the higher the carbon to water ratio, the less coke formation on the catalyst surface. Because of these advantages, APR has attracted considerable research attention in recent years, and several studies have been published on the reaction conditions, catalysts, reaction pathways, and reactor designs for APR.

Meanwhile, as various biomass-derived chemicals used for hydrogen production, ethylene glycol (C2), glycerol (C3), xylitol (C5), and sorbitol (C6) have received the most attention.

In addition, in the case of APR, hydrogen yield and selectivity are increased by using various noble metal (Pt, Pd, Ru, Rh) and non-noble metal (Ni, Co, Cu, Fe) catalysts. For example, for various noble metal catalysts (M/SiOx,) supported on silica as catalysts for the APR of ethylene glycol at 483 K and 22 bar, the catalytic activity is in the order of Pt ~ Ni > Ru > Rh ~ Pd > Ir found to decrease.

On the other hand, aluminum oxide (Al ₂ O ₃ ) as a catalyst support can be an appropriate candidate for APR because it has a strong interaction with metal active sites. As a result of examining the effect of various supports on the Pt-based catalyst on the APR of glycerol, the catalyst activity according to the type of support increased in the order of SAPO-11 zeolite < activated carbon < H-USY zeolite < SiO ₂ < MgO < Al ₂ O ₃ In particular, Pt/Al ₂ O ₃ has slightly lower hydrogen selectivity than Pt/MgO, but catalyst deactivation was not observed when Pt/Al ₂ O ₃ was used under APR reaction conditions.

On the other hand, in addition to the APR of the polyols described above, APRs that utilize lignocellulosic biomass such as xylose (C5) or glucose (C6) can utilize the richness of plant forms and non-edible lignocelluloses. It is important in that there is

However, when xylose (C5) is used, little has been reported about the APR of xylitol using Pt/C or Pt/Al ₂ O ₃ .

Embodiments of the present invention are intended to provide a catalyst for xylose reforming reaction that has excellent catalytic activity and can produce high-purity hydrogen in large quantities at low cost.

In one embodiment of the present invention, a support; and metal particles dispersed on the support, wherein the metal particles have an average diameter of 3 nm or less.

In one embodiment, the metal particle may be a platinum (Pt) particle having an oxidation number of 0.

In one embodiment, the metal particles may have an average diameter of 0.8 to 1.4 nm.

In one embodiment, the metal particles may be included in an amount of 0.1 to 10% by weight based on the total weight of the catalyst for the xylose reforming reaction.

In one embodiment, the catalyst for the xylose reforming reaction may have a pore volume of 0.1 to 2.0 cm ³ /g and a pore diameter of 50 to 200 Å.

In one embodiment, the catalyst for the xylose reforming reaction may have a BET surface area of 50 to 500 m ² /g.

In one embodiment, the catalyst for the xylose reforming reaction may not have a peak on the (111) plane on the 2θ scale of the XRD-analysis result.

In one embodiment, the catalyst for the xylose reforming reaction may have a TPR peak maximum value in the range of 130-190 °C in ammonia elevated temperature desorption (NH ₃ -TPD) analysis.

In one embodiment, the catalyst for the xylose reforming reaction has a weak acid site peak intensity 3 times or more and a middle acid site peak intensity 3 times or more and 1.5 times or more compared to platinum (Pt) in ammonia thermal desorption method (NH ₃ -TPD) analysis , The peak of the weak acid region and the peak of the intermediate acid region may appear in the region of less than 250 ° C. and the region of 250 ° C. or more and less than 500 ° C.

In another embodiment of the present invention, supporting the metal particles on the support; and reducing and activating the metal particles, wherein the metal particles have an average diameter of 3 nm or less.

In one embodiment, the metal particles may be redispersed in the activation step.

In one embodiment, the supporting step may include wet impregnation by mixing the dispersion solution and the active ingredient precursor.

In one embodiment, the activation step may change the chemical properties of the heterogeneous catalyst surface by adjusting the activation temperature or reducing conditions including atmospheric gas composition.

In one embodiment, the activation step may be reducing at a temperature of 100 to 400 ℃.

The catalyst for the xylose reforming reaction according to an embodiment of the present invention includes highly dispersed nano-metal particles and may have high activity for the APR reaction of xylose, and may have high hydrogen selectivity and conversion rate.

1 shows a schematic diagram of an autoclave reactor to which a catalyst for xylose reforming reaction according to an embodiment of the present invention is applied.
2 shows a schematic diagram of a continuous fixed bed hybrid reactor to which a catalyst for xylose reforming reaction according to an embodiment of the present invention is applied.
Figure 3 shows the pore size distribution of catalyst samples of Examples and Comparative Examples according to the present invention.
4 shows TEM images, HAADF-STEM images, and Pt particle size distributions of catalyst samples of Examples and Comparative Examples according to the present invention.
5 shows XRD patterns of catalyst samples of Examples and Comparative Examples according to the present invention.
6 shows TPR profiles of catalyst samples of Examples and Comparative Examples according to the present invention.
7 shows NH ₃ -TPD profiles of catalyst samples of Examples and Comparative Examples according to the present invention.
Figure 8 shows the results of measuring the catalyst activity by applying the catalyst samples of Examples and Comparative Examples according to the present invention to a batch reactor (autoclave).
9 shows STEM images and EDX spectra after reaction of catalyst samples of Examples and Comparative Examples according to the present invention.
10 shows the results of measuring catalyst activity by applying catalyst samples of Examples and Comparative Examples according to the present invention to a continuous fixed bed hybrid reactor.

Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings. Embodiments of the present invention have been described with reference to the accompanying drawings, but this is described for illustrative purposes, whereby the technical spirit of the present invention and its configuration and application are not limited.

The present invention can have various changes and can have various forms, the embodiments are not intended to limit the present invention to a specific disclosed form, and all changes, equivalents or substitutes included in the spirit and technical scope of the present invention It will be understood to include.

Singular expressions include plural expressions unless the context clearly dictates otherwise. In this application, the terms "include" or "have" are intended to designate that there is a feature, number, step, operation, component, part, or combination thereof described in the specification, but one or more other features It should be understood that the presence or addition of numbers, steps, operations, components, parts, or combinations thereof is not precluded.

Catalyst for xylose reforming reaction

In one embodiment of the present invention, a support; and metal particles dispersed on the support, wherein the metal particles have an average diameter of 3 nm or less.

In particular, the catalyst for the xylose reforming reaction may have excellent activity by including small-sized metal particles. For example, the metal particles may have an average diameter of 2.5 nm or less, 2.0 nm or less, 0.6 to 2.2 nm, and preferably 0.8 to 1.4 nm. When the average diameter of the metal particles exceeds 3 nm, selectivity or activity of the catalyst may be low in the xylose reforming reaction.

In one embodiment, the metal may include platinum (Pt). Meanwhile, the metal particles dispersed on the support may be platinum particles having an oxidation number of 0, which may be obtained through a reduction process.

Meanwhile, in one embodiment, the catalyst for the xylose reforming reaction may have an acid site on the surface, and the acid site may affect catalytic efficiency. Specifically, in the ammonia temperature desorption method (NH ₃ -TPD) analysis, a peak of <250 ° C may represent a weak acid region, a peak of <500 ° C may represent a medium acid region, and a peak of > 500 ° C may represent a strong acid region. The catalyst for the xylose reforming reaction may have more weak acid sites and intermediate acid sites than platinum (Pt).

For example, the catalyst for the xylose reforming reaction has a weak acid site peak intensity of 3 times or more (preferably 3.5 times or more) and a middle acid site peak intensity of 1.5 times or more compared to platinum in ammonia thermal desorption (NH ₃ -TPD) analysis. can have strength. In this way, it can have excellent catalytic efficiency by having a large number of weak acid sites and intermediate acid sites compared to platinum.

In one embodiment, the metal particles may be included in an amount of 0.1 to 10% by weight based on the total weight of the catalyst for the xylose reforming reaction. The metal particles may be supported on a support. For example, 1 to 9% by weight, 2 to 8% by weight, 3 to 7% by weight, or 4 to 6% by weight of the metal particles may be included. When the supported amount of the metal particles is less than 0.1% by weight, the amount of noble metal may be small and may not be active in the reforming reaction, and when the amount exceeds 10% by weight, the redispersion effect may be insufficient due to the interaction between metals.

In one embodiment, the catalyst for the xylose reforming reaction may have a pore volume of 0.1 to 2.0 cm ³ /g and a pore diameter of 50 to 200 Å. Specifically, the pore volume may be 0.5 to 2.0 cm ³ /g or 0.5 to 1.0 cm ³ /g, and the pore diameter may be 100 to 200 Å or 100 to 150 Å. When the pore volume and pore diameter are within the above-mentioned range, the value is about 3 times higher than that of the conventional Pt catalyst, and the loss of pore volume is minimized, so that the pores of the catalyst may not be clogged.

In one embodiment, the catalyst for the xylose reforming reaction may have a BET surface area of 50 to 500 m ² /g. Preferably, it may have a BET surface area of 100 to 400 m ² /g or 200 to 300 m ² /g. Pt particles may be highly dispersed and supported on the g-Al ₂ O ₃ support within the above-described surface area range.

In one embodiment, the catalyst for the xylose reforming reaction may not have a peak on the (111) plane on the 2θ scale of the XRD-analysis result. XRD for particles with a size of less than 2 nm does not reveal the characteristics of these particles due to their small size, so through this, the catalyst for xylose reforming reaction according to an embodiment of the present invention has a significantly small size of Pt particles, thereby achieving excellent catalytic performance can have

In one embodiment, the catalyst for the xylose reforming reaction may have a peak maximum value in the range of 130-190 ° C. On the other hand, a conventional catalyst having larger-sized Pt particles shows two peaks at 227 ° C and 347 ° C in the temperature profile, and may have Pt reducibility of the catalyst for xylose reforming reaction according to the present invention at a lower temperature. .

Method for preparing a catalyst for xylose reforming reaction

In another embodiment of the present invention, supporting the metal particles on the support; and reducing and activating the metal particles, wherein the metal particles have an average diameter of 3 nm or less.

The method for preparing the catalyst for the xylose reforming reaction may include a configuration substantially overlapping with the above-described catalyst for the xylose reforming reaction, and a detailed description thereof will be omitted.

In one embodiment, the metal particles may be redispersed in the activation step. Specifically, in the activation step, the support on which the metal particles are supported may be calcined and reduced by heat treatment. In this process, the supported metal particles may be redispersed to have a high degree of dispersion, and at the same time, the size of the metal particles may decrease. For example, in the activation step, the metal particles can be redispersed stepwise as follows: [PtCl ₆ ] ^2- +[PtCl ₅ ] ^- → PtCl ₄ → PtCl ₂ .

Through the reduction process, the metal particles supported on the support may be reduced. For example, all Pt particles may be reduced to Pt metal (oxidation number: Pt 0 valency) while undergoing a high-temperature reduction process.

In one embodiment, the supporting step may include wet impregnation by mixing the dispersion solution and the active ingredient precursor.

In one embodiment, the activation step may change the chemical properties of the heterogeneous catalyst surface by adjusting the activation temperature or reducing conditions including atmospheric gas composition. The atmosphere gas may include H ₂ gas and may be reduced to the H ₂ atmosphere gas. Also, the atmosphere gas may include Air and N ₂ gas, and calcining may be performed using the Air and N ₂ atmosphere gas. For example, N ₂ gas or the like may be injected to create the inert atmosphere.

In one embodiment, the activation step may be reducing at a temperature of 100 to 400 ℃. If the temperature is less than 100 ° C, the metal particles may not be smoothly fixed and redispersed on the surface of the metal oxide support, and if it exceeds 400 ° C, PtCl ₂ → PtO change and activity is reduced due to aggregation between metal particles at the same time It can be.

Example

Hereinafter, the present invention will be described in more detail through examples. These examples are only for illustrating the present invention, and it will be apparent to those skilled in the art that the scope of the present invention is not to be construed as being limited by these examples.

Example: Pt-SNP Preparation

It was prepared by supporting Pt nanoparticles on a γ-alumina support (γ-Al ₂ O ₃ ) using a general incipient wetness impregnation method (IWI).

γ-Al ₂ O ₃ (1/8" pellets, Alfa Aesar) was first uniformly pulverized to obtain γ-Al ₂ O ₃ (<250 mm) powder was obtained. As a Pt precursor solution, a mixture of a chloroplatinic acid solution (8wt% in H ₂ PtCl ₄ , H ₂ O, Sigma-Aldrich) and 4.5 mL of deionized water was used.

Then, the Pt precursor solution (2.0 mL) was added dropwise to the prepared γ-alumina support, and the resulting catalyst powder was dried in a vacuum oven at 100° C. for 30 minutes. This process was repeated a total of three times, and as a final step, the catalyst powder was dried again at room temperature overnight.

The catalyst powder was then calcined at a temperature of 350 °C for 2 h under air using a ramp rate of 5 °C/min, followed by 20% H ₂ /N ₂ (100 mL/min) to bring the temperature to 250 °C. and calcined for 2 hours (ramp rate of 5 °C/min) to prepare Pt nanoparticles supported on γ-alumina support (γ-Al ₂ O ₃ ) ('Pt-SNP').

Comparative Example: Pt-commercial manufacturing

For comparison, Pt/γ-Al ₂ O ₃ (Pt loading of 4.8-5.2 wt%) was purchased from Sigma-Aldrich and prepared by reduction under the same conditions as in Example ('Pt-commercial').

Experimental Example 1: Physical Characteristic Analysis of Catalyst

BET surface area, pore properties

The BET surface area, pore volume and pore size of the catalysts prepared in Examples and Comparative Examples were analyzed through N ₂ adsorption experiments, and the results are shown in Table 1 below.

Sample Pt loading (wt%) BET surface area (m ² /g) Pore volume (cm ³ /g) Pore size (Å) Average particle size (nm) Pt/γ-Al ₂ O ₃ (commercial) 5.1 ± 0.5 94.5 0.23 92.7 4.0 ± 0.8 (SD) Pt/γ-Al ₂ O ₃ (SNP) 5.9 ± 0.5 243.2 0.72 114.4 1.3 ± 0.2 (SD) γ-Al ₂ O ₃ (SNP) N/A 254.3 0.76 119.6 N/A

As a result, both the BET surface area and pore volume of the Pt-SNP catalyst were found to be almost three times higher than that of the Pt-commercial catalyst. This is believed to be due to the highly dispersed Pt particles in the γ-Al ₂ O ₃ support of the Pt-SNP, which can be confirmed by the small decrease in surface area and pore volume after Pt impregnation. As shown in Table 1, it can be confirmed that the pore volume shows only a small loss of 0.04 cm ³ /g after the deposition of the Pt particles, which indicates that there is no clogging of the catalyst pores.

Similar results are also shown in Figure 3. Comparing the pore size plots shown in Figure 3, it can be seen that the Pt-commercial has much larger particles with a large standard deviation value, while the Pt-SNP catalyst has an average of ~ 1.3 particles. . However, the total Pt loading of the two Pt catalysts was approximately 5%, indicating that the Pt particles were more uniformly dispersed on the support in the case of the Pt-SNP catalyst.

Pt particle size and distribution characteristics

The Pt particle size in the catalysts of Examples and Comparative Examples was analyzed using transmission electron microscopy (TEM) and HAADF-STEM imaging techniques, and the resulting images are shown in FIG. 4 . As can be seen in the TEM image, it can be seen that very small Pt metal is evenly dispersed on the alumina support on the catalyst surface.

In the case of the comparative example ('Pt-commercial'), polyhedral Pt particles with a size of 4-5 nm were mainly observed. The images show that the Pt particles are significantly distributed on the γ-Al ₂ O ₃ support and vary in size from 2.5 nm to 8 nm (Fig. 4a and b). The average particle size here was calculated to be about 4.0 nm with a standard deviation of 0.8.

On the other hand, in the case of the example (Pt-SNP), the Pt particles had an average size of 1.3 nm. Particles of less than 1 nm were also observed, and it was confirmed that they were stably maintained through the oxidation/reduction pretreatment process at high temperatures. Here, in the case of the Pt-SNP catalyst, the particle size distribution showed a narrow distribution curve in the range of 0.6 nm to 2.2 nm. In particular, most of the particles are distributed in the range of 0.8-1.4 nm, and through this, it can be confirmed that the catalysts according to the Examples include considerably smaller Pt nanoparticles uniformly dispersed in the γ-Al ₂ O ₃ support than the Comparative Example. have.

XRD analysis

5 shows XRD patterns of catalyst samples according to Examples and Comparative Examples. In both samples, three peaks are observed at 36.6°, 45.8° and 67.3°, which are (311), (400) and (440), respectively, typical of the γ-Al ₂ O ₃ phase. In particular, a peak appears at 39.7 ° for Pt (111), through which the presence of Pt metal can be confirmed.

On the other hand, the Pt-SNP catalyst sample had Pt particles of a considerably small size, and therefore, a peak corresponding to Pt metal (111) was not observed. It can be seen that these results are in good agreement with the TEM / STEM results because the XRD for particles with a size of less than 2 nm does not reveal the characteristics of these particles due to their small size. Therefore, it can be confirmed that considerably small Pt nanoparticles were formed on the Pt-SNP catalyst.

On the other hand, in the case of the catalyst after the catalysis, the aggregation of Pt particles during the APR reaction was confirmed in both samples.

Experimental Example 2: Catalyst Reduction Behavior Analysis

TPR experiments were performed to confirm the reduction behavior of Pt particles for the catalysts of Examples and Comparative Examples.

As can be seen in FIG. 6, the Pt reduction temperature of Pt-SNP is significantly lower than that of Pt-commercial, indicating that the reducibility of Pt nanoparticles is higher than that of larger-sized Pt nanoparticles.

From this, considering the Pt particle size of 1.3 nm in the Pt-SNP, most Pt species are likely to exist as PtCl ₂ /PtO _x on the surface and can be easily reduced compared to bulk PtO _x .

On the other hand, Pt-commercial showed two peaks at 227 °C and 347 °C in the temperature profile. Here, the first peak is related to the decrease of bulk PtO _x and the second peak is related to the decrease of PtO _x that strongly interacts with g-Al ₂ O ₃ .

Experimental Example 3: Measurement of acidity of catalyst

NH ₃ -TPD was performed to confirm the difference in acidity between the catalysts of Examples and Comparative Examples.

As shown in FIG. 7, in the case of the Pt-SNP catalyst, the total acidity estimated based on the amount of desorbed NH ₃ is slightly higher, and among all acidic sites on the catalyst surface, weak acid (<250 °C) and medium acid (<500 ℃) sites are present more than the Pt-commercial catalyst. On the other hand, the distribution of strong acid sites (> 500 °C) was similar in both samples, and in both cases, the concentration of strong acid sites was lower than that of other acid sites.

Specifically, the Pt-SNP catalyst showed a weak acid:medium acid:strong acid=23:65:12, while the Pt-commercial showed a distribution of peak intensities of weak acid:medium acid:strong acid=12:69:19, The peak intensity of the Pt-SNP catalyst was divided by the peak intensity of Pt-commercial to obtain a value, and the distribution of acidic sites was quantitatively compared.

As a result, the peak intensity of the weak acid part was about 3.6 times and the peak intensity of the middle acid part was about 1.7 times, compared to Pt-commercial, but the peak intensity of the strong acid part was about 1.14 times.

Relatedly, it is known that increasing the total acidity of Lewis and Brønsted acid sites has a significant effect on product distribution under APR reaction conditions by increasing the extent of dehydration/dehydrogenation reactions involving CO bond cleavage. In particular, it is known from previous studies that an increase in the number of weak Brønsted acid sites in the SiO ₂ -Al ₂ O ₃ support results in the formation of a smaller Pt crystallite size of less than 5 nm and a higher methane selectivity during the APR of ethylene glycol. , which is in good agreement with the measured result of higher methane selectivity for Pt-SNP catalysts compared to Pt-commercial.

Experimental Example 4: Measurement of Catalyst Activity (Autoclave)

The reforming reactivity of the catalysts of Examples and Comparative Examples was evaluated in a batch reactor (autoclave reactor), and the results are shown in FIG. 8.

As a result of comparing the catalytic activity, it was confirmed that the Example (Pt-SNP catalyst) had a significantly better effect than the Comparative Example (Pt-commercial catalyst) under APR reaction conditions.

First, in the case of the Pt-SNP catalyst, it can be confirmed that the amount of gas generated during the reaction is large. Specifically, it can be seen that the conversion rate calculated from the gas production rate curve (Figs. 8a-2 and 8b-2) is about 41%, which is significantly higher than 23.7% of the Pt-commercial catalyst.

In addition, it can be confirmed that the Pt-SNP has a higher hydrogen selectivity than the Pt-commercial catalyst. Specifically, in the case of the Pt-commercial catalyst, the initial hydrogen selectivity was almost 50%, but it can be seen that it decreases to 10-15% as the reaction proceeds. On the other hand, in the case of Pt-SNP, it was confirmed that 36% hydrogen selectivity was obtained at the beginning of the reaction and increased to 40% at the end of the reaction.

Experimental Example 5: Measurement of catalyst activity (CFR)

The catalysts according to Examples and Comparative Examples were applied to a continuous fixed bed hybrid reactor including a reformer and a hydrogen separation membrane to confirm applicability to a commercial APR process. The CFR reactor system may refer to FIG. 2 .

As in the batch reactor of Experimental Example 4, it can be seen that the catalytic activity obtained through the CFR system also agrees well with Experimental Example 4. Specifically, it was confirmed that gas having 50% hydrogen and 9% methane selectivity could be stably produced for 19 hours (FIG. 10a), thereby confirming the high stability of the Pt-SNP catalyst.

No other alkane gases were observed when compared to the results from the semi-batch reactor, which seems to be related to the nature of the CFR reactor system, which has a shorter residence time in the reactor, which lowers the possibility of gaseous by-product formation.

The embodiments of the present invention described above should not be construed as limiting the technical spirit of the present invention. The protection scope of the present invention is limited only by the matters described in the claims, and those skilled in the art can improve and change the technical idea of the present invention in various forms. Therefore, these improvements and modifications will fall within the protection scope of the present invention as long as they are obvious to those skilled in the art.

Claims (14)

As a catalyst for xylose reforming reaction,
support; And metal particles dispersed on the support; includes,
The metal particles are platinum (Pt) particles with an oxidation number of 0 and have an average diameter of 3 nm or less,
The catalyst for the xylose reforming reaction has a TPR peak maximum value in the range of 130-190 ℃ in the hydrogen temperature reduction method (TPR) analysis, the catalyst for the xylose reforming reaction. delete According to claim 1,
The metal particles have an average diameter of 0.8 to 1.4 nm, xylose reforming reaction catalyst. According to claim 1,
A catalyst for xylose reforming reaction comprising metal particles in an amount of 0.1 to 10% by weight based on the total weight of the catalyst for reforming xylose reaction. According to claim 1,
The catalyst for the xylose reforming reaction has a pore volume of 0.1 to 2.0 cm ³ /g and a pore diameter of 50 to 200 Å. According to claim 1,
The catalyst for the xylose reforming reaction has a BET surface area of 50 to 500 m ² /g. According to claim 1,
The catalyst for the xylose reforming reaction is a catalyst for the xylose reforming reaction in which the peak of the (111) plane is not observed on the 2θ scale of the XRD analysis result. delete According to claim 1,
The catalyst for the xylose reforming reaction has a weak acid site peak intensity of 3 times or more and a middle acid site peak intensity of 1.5 times or more compared to a platinum catalyst (Pt/Al ₂ O ₃ ) in ammonia elevated temperature desorption method (NH ₃ -TPD) analysis. Have,
The weak acid site peak and the intermediate acid site peak appear in the region of less than 250 ° C. and in the region of 250 ° C. to less than 500 ° C., the xylose reforming reaction catalyst. A method for preparing the catalyst for a xylose reforming reaction of any one of claims 1, 3 to 7, and 9,
supporting metal particles on a support; and
Including; reducing and activating the metal particles,
The metal particles have an average diameter of 3 nm or less, a method for preparing a catalyst for a xylose reforming reaction. According to claim 10,
A method for preparing a catalyst for a xylose reforming reaction in which metal particles are redispersed in the activation step. According to claim 10,
The supporting step is a method for preparing a catalyst for a xylose reforming reaction in which a dispersion solution and an active ingredient precursor are mixed and wet impregnated. According to claim 10,
Wherein the activation step changes the chemical properties of the catalyst surface for xylose reforming reaction by adjusting reducing conditions including activation temperature or atmospheric gas composition. According to claim 10,
The activation step is reduced at a temperature of 100 to 400 ° C., a method for preparing a catalyst for a xylose reforming reaction.

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