KR20030013153A - Metal/Al-MCM-41 Bi-functional Catalysts and manufacturing method of thereof, Applications for Hydrogenation of Aromatic Hydrocarbons using Metal/Al-MCM-41 Bi-functional Catalysts - Google Patents

Abstract

PURPOSE: Provided are a metal/Al-MCM-41 binary catalyst and a hydrogenation of unsaturated hydrocarbon using the metal/A1-MCM-41 binary catalyst in which weight ratio of a metal to Al-MCM-41 is about 0.001 to 0.15, and the metal is selected from a group comprising platinum (Pt), palladium (Pd) and nickel (Ni) in the periodic table. CONSTITUTION: The metal/Al-MCM-41 binary catalyst fabrication method comprises the steps of (a) obtaining alkali metal silicate aqueous solution by making silica react with alkali metal aqueous solution, (b) dropping the alkali metal silicate aqueous solution to a template and obtaining an MCM-41 substrate by hydrothermal synthesis of the mixed aqueous solution at pH of 9-11, (c) adding aluminum (Al) precursor dissolved in organic solvent to the MCM-41 substrate, agitating the mixture, and obtaining precipitant, (d) sintering the precipitant obtained during the step (c) at a temperature of 300-800°C for 1-48 hours, thereby obtaining Al-MCM-41, (e) impregnating a metal precursor of a group VIII in the periodic table into the Al-MCM-41 and sintering the metal-impregnated Al-MCM-41 at a temperature of 150-600°C for 1-48 hours.

Description

Metal / Aｌ-MCM-41 binary catalyst and preparation method thereof, and hydrogenation reaction of unsaturated hydrocarbon using metal / Aｌ-MCM-41 binary catalyst {Metal / Al-MCM-41 Bi-functional Catalysts and manufacturing method of Hydrogenation of Aromatic Hydrocarbons using Metal / Al-MCM-41 Bi-functional Catalysts}

The present invention relates to a metal / Al-MCM-41 binary catalyst and a preparation method thereof and to hydrogenation of unsaturated hydrocarbons using a metal / Al-MCM-41 binary catalyst.

Dearomatization of the hydrogenation of unsaturated hydrocarbons refers to a process in which an aromatic component mixed in an oil component is reacted with hydrogen on a catalyst to be converted to naphthene and removed.

In general, light oils have boiling points in the range of 200 ° C to 370 ° C and point out the fraction of the oil spilled after kerosene during crude oil distillation. Light oils must satisfy the properties of adequate ignition, pour point, viscosity, startability, etc. The combustion of diesel engines using light oil as a raw material tends to be delayed a little time until the ignition occurs after spontaneous ignition by compressed air or after fuel is injected. If this ignition time becomes long, the pressure of combustion gas will rise and a sudden combustion will cause an impact (diesel knock). A cetane number is used as a measure of the flammability of light oils.

Cetane number is a CFR engine for measuring cetane number based on the flammability of cetane standard fuel prepared by mixing cetane number of cetane with good flammability as 100 and cetane number of heptamethyl nonane with low flammability as 15. Measure The relationship between cetane number and hydrocarbon composition is roughly linear paraffin> isoparaffin> naphthene> olefin> aromatics. As the content of aromatic compounds in the light oil increases, the cetane number decreases. For example, cetane number is -15 of naphthalene, tetrahydronaphthalene (tetralin), 7 decahydronaphthalene (decalin), 48 of butylcyclohexane, and 76 of decane. Therefore, saturation of aromatic components in light oil and conversion to cyclic compounds under conditions without severe cracking results in light oil quality improvement. In addition, aromatic compounds do not directly increase the emissions of NOx but lower the cetane number, that is, lower the combustion efficiency, and consequently increase the emissions of NOx. For this reason, the dearomatic process of light oils increases the cetane number of light oils and results in a reduction of NOx emissions. Aromatic compounds have a lower specific gravity than paraffinic compounds with the same boiling point as the API (American Petroleum Institute). The dearomatic process of the light oil is to convert to a compound with a large API specific gravity, thus increasing the volume yield of the oil.

In addition, aromatic compounds have their own carcinogenic properties, which are unburned in the light oil phase and emitted in the form of dust in the atmosphere, which has a detrimental effect on the environment and the human body. As a result, the regulation of aromatics in light oils is expected to become more stringent, especially in developed countries such as the United States and the European Union. In order to produce environmentally friendly light oils, much of the aromatics must be removed.

Catalysts used for the dearomatic process of light oil can be classified into two types of transition metal sulfide catalysts and noble metal catalysts. In the case of the metal sulfide catalyst, the Ni-Mo catalyst has better dearomatic activity than the Co-Mo catalyst, and the Ni-W catalyst has higher activity than the Ni-Mo catalyst when the sulfur content of light oil is low. However, metal sulfide catalysts do not have sufficient activity to obtain dearomatized diesel fuel at normal pressure conditions. Increasing the reaction temperature increases the activity but has the disadvantage of decreasing the life of the catalyst. Precious metal catalysts are known to have better hydrogenation activity than metal sulfide catalysts and there are many processes using such catalysts. However, the noble metal catalyst has a low endothelial toxicity to sulfur components contained in the light oil, resulting in a drastic decrease in activity. Therefore, it is necessary to develop a noble metal catalyst having resistance to sulfur, and it is reported that the introduction of an acid point into the carrier can increase the sulfur resistance. Precious metals loaded on a carrier with acidic points cause electron-deficient phenomena in which the charges have a positive charge, in part by the acidic point. It can increase the resistance to. However, the catalyst having an acidic point is also used as a catalytic cracking catalyst by itself, there is a disadvantage that the yield of the product is reduced when the catalytic decomposition reaction occurs. Therefore, the scattering of the appropriate intensity is required.

The catalyst development for the dearomatic reaction is an attempt to use a zeolite having a large surface area and a molecular sieve having a pore of molecular size, and ZSM-5, Beta zeolite (Amoco corp., USP 5,494,870), Y zeolite ( Attempts to apply binary catalysts prepared by supporting metals on zeolite carriers such as Shell Oil Corp., USP 5,391,291) and mordenite (Amoco Corp., USP 5,225,383) and amorphous carriers such as silica-alumina and alumina for dearomatic reactions Are actively being done.

There are reports of supporting Pt-Pd as a bimetallic instead of using Pt or Pd alone as an attempt to improve the metal point to increase the sulfur resistance.

Therefore, the need to overcome the disadvantages of the prior art, and to develop a catalyst capable of producing a catalyst capable of effectively hydrogenating aromatic compounds, such as naphthalene in light oil, sulfur resistance.

Accordingly, the present inventors earnestly endeavored to develop a method for producing a catalyst having excellent dearomatization performance, and thus, obtained a high hydrothermal stability MCM-41 carrier during the manufacturing process of the metal / Al-MCM-41 catalyst. When Al and metal were supported by the post-treatment method, it was confirmed that a binary catalyst having good conversion of naphthalene even in the presence of sulfur was produced, and thus, the present invention was completed.

After all, the main object of the present invention is to provide a method for producing a metal / Al-MCM-41 catalyst and a metal / Al-MCM-41 catalyst, and also to use the metal / Al-MCM-41 catalyst for hydrogenation of unsaturated hydrocarbons. will be.

1 is a graph showing the conversion rate of naphthalene over time of Pt / Al-MCM-41 catalyst.

2 is a graph showing the conversion activity of naphthalene in the presence of sulfur over time of Pt / Al-MCM-41 (5) -Post catalyst.

Method for producing a metal-containing binary catalyst of the present invention comprises the steps of reacting silica with an aqueous alkali metal solution to obtain an alkali metal silicate aqueous solution; Adding an aqueous alkali metal silicate solution to the template material and hydrothermally synthesizing to obtain an MCM-41 carrier; Adding an aluminum (Al) precursor dissolved in an organic solvent to the MCM-41 support and stirring to calcinate the resulting precipitate to obtain Al-MCM-41; And impregnating the Al-MCM-41 with a precursor solution of the Group VIII metal to support the Group VIII metal, followed by calcination.

On the other hand, the hydrogenation method of saturating unsaturated hydrocarbons using a metal-containing binary catalyst prepared by the above method comprises the steps of reducing the metal-containing binary catalyst by putting a metal-containing binary catalyst in a high-pressure reactor and reacted with hydrogen; Injecting an oil comprising an unsaturated hydrocarbon into the electroreduced metal-containing binary catalyst and then reacting with hydrogen to saturate the unsaturated hydrocarbon.

Hereinafter, the method for preparing the metal-containing binary catalyst of the present invention will be described in more detail by dividing the process.

First Step: Alkali Metal Silicate Aqueous Solution Preparation

The silica is reacted with an aqueous alkali metal solution to obtain an aqueous alkali metal silicate solution, which is used to disperse the silica well in a monomer state. At this time, the ratio of the amount of alkali metal and silica (Alkali metal / Si) is about 0.1-5 in element ratio, preferably 0.3-0.7, and the concentration of the aqueous alkali metal solution is 0.1-5 molar concentration. If the molar concentration is 0.5-1 and the alkali metal ratio is less than 0.1 molar concentration, the silica will not be dispersed well with the monomer. If the molar concentration is more than 5 molar concentration, the alkali metal ratio is too high in the MCM-41 synthesis, so that the hydrothermal synthesis may not be good. have. In this case, one or more materials selected from fumed silica, aerosil, and tetraorthosilicate may be used, and preferably, Ludox HS-40 (Ludox) by DuPont. HS-40), or silica sold under the trade name Ludox AS-40. Alkali metal refers to an element belonging to group 1A in the chemical periodic table, preferably one selected from lithium (Li), sodium (Na), and potassium (K), more preferably sodium. .

Second Step: MCM-41 Carrier Preparation

The aqueous alkali metal silicate solution obtained in the first step was added dropwise to the aqueous solution of the template material and hydrothermally synthesized to prepare an MCM-41 carrier. At this time, the template material is a chemical substance that has a uniform pore shape by helping to form a colloidal particle (micelle), which is a chemically stable intermediate in the synthesis of a carrier. In this case, the molar ratio of hydrogel used is 1.0CTACl-1.0Na ₂ O-4.0SiO ₂ -400H ₂ O, and CTACl refers to hexadecyltrimethylmethylammonium chloride, which is one of the template materials. It is not. In the present invention, octadecyltrimethylammonium bromide, cetyltrimethylammonium chloride, myristyltrimethylammonium chloride, dodecyltrimethylammonium bromide, and decyltrimethylammonium bromide (decyltrimethylammonium bromide), octyltrimethylammonium bromide, hexyltrimethylammonium bromide, or a mixture thereof is used, respectively.

Hydrothermal synthesis is used to accelerate the growth of crystals by applying heat to a mixture containing water. The hydrothermal synthesis is carried out by placing the mixture in an airtight container and raising the temperature to react under pressure. At this time, MCM-41 has a disadvantage in that it breaks at high temperature in a moist condition. As a means to solve the problem, the pH of the reaction solution is maintained at 9 to 11 by adding a conventional acid such as hydrochloric acid and acetic acid or a diluent thereof. It is preferable to do this, and this can be done repeatedly.

After the hydrothermal synthesis is completed as described above, the precipitate is filtered, washed, and dried in a conventional manner to obtain an MCM-41 carrier. At this time, the pore size of the carrier can be adjusted by varying the mold material, the pore size of the carrier is preferably 1.5 to 20nm in average diameter. When the average diameter is less than 1.5 nm, it is difficult for the surfactant to form colloidal particles in the liquid mixture, and thus, the pore structure is difficult to develop and grow. When the average diameter exceeds 20 nm, the pores of the MCM-41 are difficult to form and the lattice stability is poor. There is a problem that the structure is easily collapsed.

Third Step: Preparation of Al-MCM-41 Carrier

In order to graf the aluminum to the MCM-41 carrier, the moisture of the carrier prepared in the second step should be sufficiently dried under vacuum or normal pressure at a temperature of 100-140 ° C to remove the moisture therein. An aluminum precursor dissolved in an organic solvent was added, stirred, and the resulting precipitate was calcined to prepare an Al-MCM-41 carrier. The amount used is 10-1000 ml of organic solvent per gram of carrier, preferably 100-300 ml per gram. When the amount of organic solvent is too small, the precursor is not completely dissolved and it is easy to mix with the carrier. If the amount of the organic solvent is too large, the excessive amount of solvent is used, there is a disadvantage in that the filtration time increases. In this case, the organic solvent may be ethanol, methanol, propanol, acetone, or a mixed solution thereof, but it is preferable to use ethanol having a relatively low toxicity and high solubility in metal precursors.

AlCl ₃ , Al (OH) ₃ , Al (OCH ₃ ) ₃ may be used as the aluminum precursor, or a mixture thereof may be used, and AlCl ₃ having excellent reactivity is preferable. The amount of aluminum precursor used at this time

The addition amount of the aluminum precursor is preferably added so that the molar ratio of Si / Al of Al-MCM-41 finally produced is 1 to 200. When the molar ratio of Si / Al does not reach 1, that is, when aluminum is introduced in a large amount, Al is not introduced into the lattice of MCM-41, but is alumina in the form of oxide. When the molar ratio of Si / Al exceeds 200, the amount of acid point introduced is low, and thus the reaction activity is low, which is not preferable for the purpose of the present invention.

The resulting precipitate is filtered, washed and dried in a conventional manner and then calcined for 1 to 48 hours at a temperature of 300 to 800 ° C. If the temperature does not reach 300 ℃ during firing, the Al cannot enter the temperature enough to enter the lattice. If the firing temperature exceeds 800 ℃, the lattice of MCM-41 may collapse due to the high temperature required. Because it is not desirable. On the other hand, if the firing time does not reach 1 hour, Al is not enough time to enter the lattice. If the firing time exceeds 48 hours, the lattice of MCM-41 may collapse due to the long firing time. Not desirable

Fourth Step: Preparation of Metal / Al-MCM-41 Binary Catalyst

Al-MCM-41 is impregnated with a precursor solution of Group VIII metal to support the metal on the Al-MCM-41 carrier, and then calcined to prepare a metal / Al-MCM-41 binary catalyst. At this time, the Group VIII metal is reduced by hydrogen, which acts as an active point for the hydrogenation and dehydrogenation reaction in the metal state, and the Group VIII metal has less side reactions of platinum (Pt), palladium (Pd) or Nickel (Ni) is preferred. On the other hand, elements such as platinum, palladium or nickel cannot be supported in the solid phase and should be added to Al-MCM-41 in the form of a precursor. As the precursors of these metals, Pt (NH ₃ ) ₅ · Cl · H ₂ O, Pt _{(NH 3) 4 · Cl 2} · H 2 O, Pt (NH 3) 3 · Cl 3 · H 2 O, Pt (NH 3) 2 · Cl 4 · H 2 O, Pt (NH 3) · Cl 5 · _{H 2 O, PtCl 6, PtCl} 4, PtCl 2, PtS 2, PtSO 4, Pd (NH 3) 5 · Cl · H 2 O, Pd (NH 3) 4 · Cl 2 · H 2 O, Pd (NH 3 _{) 3 · Cl 3 · H 2} O, Pd (NH 3) 2 · Cl 4 · H 2 O, Pd (NH 3) · Cl 5 · H 2 O, PdCl 6, PdCl 4, PdCl 2, PdS 2, PdSO _{4, Ni (NH 3) 5} · Cl · H 2 O, Ni (NH 3) 4 · Cl 2 · H 2 O, Ni (NH 3) 3 · Cl 3 · H 2 O, Ni (NH 3) 2 · One or more materials selected from Cl ₄ H ₂ O, Ni (NH ₃ ) Cl ₅ H ₂ 0, NiCl ₆ , NiCl ₄ , NiCl ₂ , NiS ₂ , and NiSO ₄ are used.

The amount used is 10-500 ml of water per 1 g of Al-MCM-41 prepared in the electrical process, and the amount of metal supported is such that the ratio of metal / (metal + Al-MCM-41) is 0.0001 to 0.15 by weight. When the ratio of metal / (metal + Al-MCM-41) is less than 0.0001, there is a problem in that the cranking reaction occurs mainly due to the low hydrogenation-dehydrogenation ability due to the small metal points formed. Even if the amount of the metal increases, the amount of the metal point exposed on the surface does not increase, which is undesirable. And Al-MCM-41 supported using a precursor solution of metal is filtered and dried by conventional methods known in the art and calcined under the same conditions as in the third process.

Meanwhile, a hydrogenation method for saturating unsaturated hydrocarbons using the metal / Al-MCM-41 binary catalyst prepared by the first to fourth processes will be described in more detail by the steps.

First Step: Reduction of Metal-Containing Binary Catalysts

The metal / Al-MCM-41 binary catalyst prepared in the first to fourth steps was introduced into the high pressure reactor, and then reacted with hydrogen to reduce the metal-containing binary catalyst.

Since the metal of the metal-containing binary catalyst has an oxide form, it is necessary to reduce it to a metal form. The reduction of the metal-containing binary catalyst described above is preferably performed at a temperature of 150 ° C. to 550 ° C. and 0.1 to 10 atmospheres in a hydrogen atmosphere. If the temperature is less than 150 ℃ metal is difficult to reduce, if it exceeds 550 ℃ the metal is sintered (sintering) it is not preferable because the degree of dispersion of the metal is low.

Second Step: Hydrogenation of Unsaturated Hydrocarbons

In the first step, the reduced metal / Al-MCM-41 binary catalyst is injected with an oil containing an unsaturated hydrocarbon containing an unsaturated hydrocarbon or a sulfur compound, and then reacted with hydrogen to hydrogenate the unsaturated hydrocarbon. The unsaturated hydrocarbons that can be reduced by the hydrogenation method are naphthalene, benzene, anthracene, phenanthrene and the like, and the sulfur compound is selected from the group consisting of sulfur-containing compounds such as thiophene, benzothiophene, dibenzothiophene and diphenylbenzothiophene. Either one or more is a mixture and the concentration of sulfur compounds is up to 500 ppm (w).

Hydrogenation of these unsaturated hydrocarbons is preferably carried out under the conditions of 100 to 400 ℃, 10 to 100 atm. If the temperature is less than 100 ℃ during the hydrogenation reaction, the reaction activity is low and requires a lot of time, and if it exceeds 400 ℃, conversion to the dearomatic reaction is reduced due to thermodynamic limitation, and the linear reaction paraffin (light oil model material) as a side reaction. It is not preferable because the yield is accompanied by a cracking reaction of. The present invention will be described in more detail by the following examples. These are intended to explain the present invention in more detail, and it will be apparent to those skilled in the art that the scope of the present invention is not limited by these examples in accordance with the gist of the present invention.

Example 1 Preparation of Pt / Al-MCM-41 Catalyst

14.3 g of colloidal silica Ludox HS-40 (manufactured by DuPont, USA) was mixed with 51.5 ml of an aqueous 1 M NaOH solution and heated at 80 ° C. for 2 hours to obtain an aqueous sodium silicate solution.

Aqueous sodium silicate solution was added dropwise dropwise to a 25% by weight aqueous solution of cetyltrimethylammonium chloride with a dropper for 1 hour, and then the mixture was placed in an oven at 100 ° C. to crystallize the MCM-41 carrier in silica form by hydrothermal synthesis for 2 days. . Subsequently, the mixture was cooled to room temperature, and then the pH was adjusted to 10 with 1M CH ₃ COOH aqueous solution, followed by repeated hydrothermal synthesis. The precipitate was filtered, washed with tertiary distilled water at 80 ° C., and dried at 110 ° C. to obtain an MCM-41 carrier.

The MCM-41 carrier was sufficiently dried at 140 ° C. for 10 hours, and then 5 g of the carrier was added to 300 ml of anhydrous ethanol solution in which AlCl ₃ was dissolved, stirred well for 1 hour, filtered, washed with ethanol, dried at 110 ° C., and then dried at 550 ° C. It was calcined for 10 hours at to obtain an Al-MCM-41 carrier having a molar ratio of Si / Al of 5 to 40. At this time, the ratio of Si / Al was adjusted by varying the amount of AlCl ₃ dissolved in anhydrous ethanol.

The Al-MCM-41 support the platinum of the liquid precursor tetraamine platinum (Ⅱ) chloride, in Hyde light metal was impregnated with (tetraamineplatinum (Ⅱ) Chloride hydrate, 98%, Pt (NH 3) 4 · Cl 2 · H 2 O) Pt / Al-MCM-41 binary catalyst was prepared by complexing the platinum so that the ratio of (metal + Al-MCM-41) was 0.005 in weight ratio, and then calcining it at 320 ° C for 2 hours.

<Example 2>

0.5 g of a Pt / Al-MCM-41 catalyst (molar ratio of Si / Al of 5) prepared by the method of Example 1 was introduced into a 300 ml high-pressure reactor, followed by flowing 99.999% hydrogen at 50 cc / min and 500 The temperature of the reactor was raised to 5 ° C. per minute while stirring at rpm, followed by reaction at 320 ° C. and 1 atm for 2 hours to reduce the metal-containing binary catalyst.

50 ml of 5% (w / w) naphthalene was injected as a model reactant of a light oil containing an aromatic compound to the reduced catalyst. In this case, 20.34 g of naphthalene was dissolved in 500 ml of hexadecane and 5% (w / w). ). The temperature was raised to 5 ° C. per minute and adjusted to a reaction temperature of 200 to 300 ° C. After the temperature rose, the pressure was adjusted to 68.5 bar.

Samples were taken over time and the content of aromatic components was analyzed using a flame ionization detector of gas chromatography (HP6890) equipped with an HP-1 column.

Subsequently, in order to confirm the resistance of the catalyst to sulfur, 0.12 g of dibenzothiophene, 200 ppm (w), was mixed with 20.34 g of naphthalene and 500 ml of hexadecane to prepare a model solution. The prepared solution was injected into the reduced Pt / Al-MCM-41 catalyst as described above, followed by hydrogenation of naphthalene in a hydrogen atmosphere at 300 ° C. and 68.5 atm.

The hydrogenation process of naphthalene, as shown by the following general formula (I), first forms tetralin, and then tetralin is hydrogenated once more to form decalin to complete hydrogenation (saturation). In the present embodiment, the concentration of the reaction product and the conversion rate of naphthalene over time were measured using gas chromatography (HP6890) equipped with a flame ionization detector while the hydrogenation reaction was performed, and are shown in FIGS. 1 and 2.

General formula (Ⅰ)

<Example 3>

In preparation of Pt / Al-MCM-41 catalyst, the Pt / Al-MCM-41 catalyst was added in the same manner as in Example 1 except that the pretreatment synthesis method was added dropwise to the MCM-41 carrier, hydrothermally synthesized, and then stirred by adding an aluminum precursor. Naphthalene was hydrogenated in the same manner as in Example 2, except that a catalyst having a ratio of 5 and 40 of Si / Al was prepared and the concentration of the reaction product and the conversion rate of naphthalene were changed. Measured.

Comparative Example

The following shows the activity of the catalysts and the catalysts prepared in the present invention and the sulfur present in the literature in Table 1. As can be seen from the following, the platinum-supported catalyst (Pt / Al-MCM-41 (5) -Post) on Si-Al = 5 carrier prepared by post-treatment synthesis showed excellent sulfur resistance. .

Table 1. Conversion of Naphthalene with and without Sulfur for Various Catalysts

catalyst Reaction temperature (℃) Hwang Yumu (200ppm DBT) Time taken for naphthalene to complete conversion (h) Tetralen time taken to complete conversion (h) Remarks Pt / Al-MCM-41 (5) -Post 200 radish 6 8 Pt / Al-MCM-41 (5) -Post 300 radish 0.33 0.5 Pt / Al-MCM-41 (5) -Post 300 U 0.75 3 Highest activity in yellow presence Pt / Al-MCM-41 (5) -Pre 200 radish 6 14 Pt / Al-MCM-41 (5) -Pre 300 radish 0.5 0.5 Pt / Al-MCM-41 (5) -Pre 300 U 3 6 Pt / γ-alumina 300 radish 5 - Tetralene conversion is very slow Pt / silica-alumina 200 radish 3 4 Pt / silica-alumina 300 U 5 6 Pt / H-Y 200 radish 7 8 Pt / H-Y 300 radish 0.5 0.33 Pt / Beta 300 radish 2 2 Lots of cracking Pt / Beta 300 U 5 - Lots of cracking

As described and demonstrated in detail above, the metal-supported Al-MCM-41 binary catalyst of the present invention shows excellent performance in the process of removing aromatic compounds in the light oil. The metal-containing binary catalyst of the present invention showed high activity of hydrogenation of naphthalene even in the presence of sulfur. Therefore, the binary catalyst of the present invention can be widely used as a catalyst for dearomatic process of light oil.

Claims (16)

Metal / Al-MCM-41 binary catalyst having a weight ratio of metal / (metal + Al-MCM-41) of 0.0001 to 0.15 The metal according to claim 1, wherein the metal in the metal / Al-MCM-41 catalyst is any one of Group VIII elements on the chemical periodic table, preferably platinum (Pt), palladium (Pd) or nickel (Ni). / Al-MCM-41 binary catalyst Reacting the silica with an aqueous alkali metal solution to obtain an aqueous alkali metal silicate solution; Adding an aqueous alkali metal silicate solution to the template material and hydrothermally synthesizing at a pH of 9 to 11 to obtain an MCM-41 carrier; Adding an aluminum (Al) precursor dissolved in an organic solvent to the MCM-41 support, stirring, and calcining the resulting precipitate at a temperature of 300 to 800 ° C. for 1 to 48 hours to obtain Al-MCM-41; Metal-Al-MCM-, comprising the step of impregnating the precursor solution of the Group VIII metal to Al-MCM-41 to support the Group VIII metal and then firing for 1 to 48 hours at a temperature of 150 ~ 600 ℃ 41 Production method of binary catalyst The method of claim 3, wherein the silica is at least one material selected from fumed silica, aerosil, tetraorthosilicate, and the like. The method of claim 3, wherein the alkali metal is one selected from lithium (Li), sodium (Na), and potassium (K). The method of claim 3, wherein the template material is octadecyltrimethylammonium bromide, cetyltrimethylammonium chloride, myristyltrimethylammonium chloride, dodecyltrimethylammonium bromide, decyltrimethylammonium bromide, octyltrimethylammonium bromide, hexyltrimethylammonium bromide, respectively. Method for producing a metal / Al-MCM-41 binary catalyst characterized in that or a mixture thereof The method of claim 3, wherein the aluminum precursor is AlCl ₃ , Al (OH) ₃ , Al (OCH ₃ ) ₃ , or a mixture thereof, respectively. The precursor of Group VIII metal is Pt (NH ₃ ) ₅ .Cl.H ₂ O, Pt (NH ₃ ) ₄ .Cl ₂ .H ₂ O, Pt (NH ₃ ) ₃ .Cl ₃ .H _{2 O, Pt (NH 3)} 2 · Cl 4 · H 2 O, Pt (NH 3) · Cl 5 · H 2 O, PtCl 6, PtCl 4, PtCl 2, PtS 2, PtSO 4, Pd (NH 3) _{5 · Cl · H 2 O,} Pd (NH 3) 4 · Cl 2 · H 2 O, Pd (NH 3) 3 · Cl 3 · H 2 O, Pd (NH 3) 2 · Cl 4 · H 2 O, _{Pd (NH 3) · Cl 5} · H 2 O, PdCl 6, PdCl 4, PdCl 2, PdS 2, PdSO 4, Ni (NH 3) 5 · Cl · H 2 O, Ni (NH 3) 4 · Cl 2 _{· H 2 O, Ni (NH} 3) 3 · Cl 3 · H 2 O, Ni (NH 3) 2 · Cl 4 · H 2 O, Ni (NH 3) · Cl 5 · H 2 O, NiCl 6, NiCl ₄ , NiCl ₂ , NiS ₂ , and NiSO _{4 A} method for producing a metal / Al-MCM-41 binary catalyst characterized in that at least one material selected from 4. The method of claim 3, wherein the metal / Al-MCM-41 catalyst has a molar ratio of Si / Al of 1 to 200. Reducing the metal / Al-MCM-41 binary catalyst prepared by the method of any one of claims 3 to 9 by reacting with hydrogen; Injecting an unsaturated hydrocarbon or an unsaturated hydrocarbon containing a sulfur compound into the reduced metal / Al-MCM-41 binary catalyst; Unsaturation using a metal / Al-MCM-41 binary catalyst comprising reacting hydrogen of a metal / Al-MCM-41 binary catalyst with an unsaturated hydrocarbon containing an unsaturated hydrocarbon or a sulfur compound to hydrogenate the unsaturated hydrocarbon. Hydrogenation of Hydrocarbons The method of claim 10 wherein the unsaturated hydrocarbon is dissolved in at least one solvent selected from the group consisting of linear decane, unidecane, tridecane, tetradecane, pentadecane, hexadecane and injected into the metal / Al-MCM-41 binary catalyst. Hydrogenation of Unsaturated Hydrocarbons Using Metal / Al-MCM-41 Binary Catalysts The hydrogenation of an unsaturated hydrocarbon using a metal / Al-MCM-41 binary catalyst according to claim 10, wherein the reduction of the metal / Al-MCM-41 binary catalyst is carried out under a hydrogen atmosphere at 100 ° C. to 550 ° C. 12. Way 11. The method of claim 10, wherein the reduction of unsaturated hydrocarbons is carried out under the conditions of 100 ℃ to 400 ℃, 1 to 100 atm pressure hydrogenation method of the unsaturated hydrocarbon using a metal / Al-MCM-41 binary catalyst. According to claim 1, Unsaturated hydrocarbon is one or two or more selected from the group consisting of aromatic compounds, such as naphthalene, benzene, anthracene, pentracene, is a mixture using a metal / Al-MCM-41 binary catalyst Hydrogenation of Hydrocarbons The metal / Al- compound according to claim 10, wherein the sulfur compound is any one or two or more selected from the group consisting of sulfur-containing compounds such as thiophene, benzothiophene, dibenzothiophene and diphenylbenzothiophene. Hydrogenation of Unsaturated Hydrocarbon Using MCM-41 Binary Catalyst The method of hydrogenating unsaturated hydrocarbons using metal / Al-MCM-41 binary catalysts according to claim 10 or 15, wherein the sulfur compound has a concentration of up to 500 ppm (w).