KR19980057182A - Acetylene Selective Hydrogenation Catalyst and its preparation method - Google Patents

Abstract

The present invention relates to an acetylene selective hydrogenation catalyst and a method for preparing the same. More specifically, the present invention relates to a novel catalyst composition having a slow deactivation rate for selectively hydrogenating acetylene in acetylene containing acetylene and a method for preparing the same, in particular, 0.005 to 2.0 wt% of a hydrogenation catalyst and 0.001 to 2.0 wt% of a silicone as a modifier. The present invention relates to a catalyst composition for selectively hydrogenating acetylene contained in ethylene prepared by supporting% on at least one carrier selected from alumina, titanium dioxide, silica, and silica alumina.

Description

Acetylene Selective Hydrogenation Catalyst and its preparation method

The present invention relates to an acetylene selective hydrogenation catalyst and a method for preparing the same. More particularly, the present invention relates to a novel catalyst composition having a slow deactivation rate for selectively hydrogenating acetylene in acetylene-containing ethylene and a method for preparing the same.

Ethylene is a substance used as a monomer in the production of various kinds of polymers and is produced by pyrolysis of naphtha or catalytic catalytic cracking of petroleum gas such as ethane, propane and butane. In general, the ethylene produced by the above method contains about 0.5 to 2.0% by weight of acetylene, and to be used as a monomer for the polymer, the acetylene should be lowered to an appropriate concentration or less. In the case of ethylene having a high acetylene content, the activity of the polymerization catalyst is lowered and the physical properties of the resulting polymer material are also lowered. In the 1950s, the amount of acetylene allowed in ethylene was reduced to 50 ppm, 10 to 20 ppm in the 1960s, and recently to 2 ppm or less. It was.

As a method of removing a small amount of acetylene contained in ethylene, there is a solvent extraction method (US Pat. No. 3,755,488) and a hydrogenation method using a catalyst. In the current general process, ethylene containing about 1% of acetylene separated from the upper part of the ethylene separation column is selectively hydrogenated using a hydrogenation catalyst to produce high purity ethylene, which is known to be cheaper than solvent extraction. Various transition metals can be used as the hydrogenation catalyst, and the most important consideration in the hydrogenation reaction is selectivity in which only acetylene is selectively hydrogenated and ethylene is not hydrogenated. If the selectivity is high, the yield of ethylene is high.

As selective acetylene hydrogenation catalysts, sulfide catalysts such as nickel sulfide and nickel sulfide-tungsten or copper-based catalysts were frequently used. However, since these catalysts have low reactivity, the catalysts must be reacted at a high temperature, thereby increasing the polymerization reaction and causing clogging of catalyst pores. Thus, the catalyst has a short regeneration cycle. When noble metals are used as catalysts, improved results in reactivity and selectivity have been obtained. In particular, Pd is known to have excellent reactivity. According to Bond et al., The selectivity of the transition metal catalysts in the selective hydrogenation of acetylene is lowered in the following order (Catalysis by metals, Academic press, New York, 281-309, 1962).

Pd Rh, Pt Ni Ir

According to Trimm et al., Pd and Ni can selectively protect triple bond materials in the presence of double bond materials, and Ni has greater activity for decomposition than other metals (Design of catalysts, Elsevier, 229-248, 1980). .

In order for the transition metal catalyst used in the hydrogenation reaction to be an effective catalyst, a large surface area is required for the same amount of metal. To this end, a method of dispersing the catalyst component using a carrier is used. Another reason for dispersing the catalyst component using a carrier is to facilitate the removal of excess heat of reaction expected in commercial processes. When 1 mole of acetylene is hydrogenated to produce 1 mole of ethylene, heat of reaction of 40 kPa or more is generated. In the case of undispersed catalyst, heat of reaction is accumulated locally, which makes it difficult to control the temperature of the reactor. When the reaction temperature rises, acetylene is converted more to ethylene, but also the fraction of ethylene to ethane increases. Since the selectivity of the reaction varies depending on the reaction temperature, it is necessary to maintain an appropriate reaction temperature range and the heat of reaction must be controlled within the appropriate range. In general, it is preferable to select a catalyst and a reactor where the temperature rise is within 15 ° C. when acetylene is completely removed.

U.S. Patent No. 2,511,453 describes a method for producing a catalyst using nickel, chromium, and cobalt, and the residual acetylene concentration after hydrogenation is relatively high, such as 50 to 100 ppm.

U.S. Patent No. 2,735,897 describes a catalyst preparation process having a composition of 0.025-0.3 wt% palladium / alumina, commercialized as ICI-38-1 (ICI), G-583 (Girdler).

US Pat. No. 4,387,258 describes a catalyst preparation method for dispersing a catalyst component on a silica carrier, and US Pat. No. 4,839,329 describes a method for preparing a catalyst by dispersing palladium on a titanium dioxide carrier.

However, when preparing a hydrogenation catalyst using a carrier there is a problem due to side reactions derived by the carrier. Since the carriers used in the above patents exhibit weak acidic properties, acetylene or ethylene is polymerized to form green oil having 4 or more carbon atoms. The produced green oil blocks a portion of the catalyst pores and blocks the access of the reactants or acquires the hydrogenation active site, which causes the problem of promoting catalyst deactivation, resulting in shortening the regeneration cycle and life of the catalyst.

Many efforts have also been made to develop a method for improving the selectivity of a catalyst in acetylene selective hydrogenation. Although it is generally known that the hydrogenation rate of ethylene is 10 to 100 times faster than the hydrogenation rate of acetylene ( Adv. In Catal ., 15, 91-226 (1964)), acetylene is selectively hydrogenated. This is because it selectively adsorbs to the reaction active point and it is known that the surface reaction is not the rate step but the adsorption and desorption step. The adsorption properties of hydrogen, such as acetylene, methylacetylene, propadiene, ethylene, and propylene, on the Group 8 metals such as Pd, were found to be in the following order and desorption rates in the reverse order (The Oil and Gas Journal, 27, 66 (1972).

Acetylene Diolefin Olefin Paraffin

When diolefin is added to the hydrogenation of acetylene, ethylene can be selectively hydrogenated without hydrogenation because diolefin interferes with the adsorption of ethylene. A material having a moderate adsorption characteristic as described above is called a moderator, and carbon monoxide is known to play a role similar to that of diolephine. In the case of diolefin, carbon monoxide is known to be more suitable as a moderator because it promotes the production of green oil and there is a separation problem after the reaction.

US Pat. Nos. 3,325,556 and 4,906,800 describe methods for improving selectivity by adding trace amounts of carbon monoxide in the reactants.

The addition of trace amounts of carbon monoxide improves selectivity, but causes carbonylation reactions on the surface of the catalyst and promotes the production of green oil, a mixture of polymers with four or more carbon atoms, which promotes the deactivation of the catalyst and increases the regeneration cycle and lifetime of the catalyst. It is shortened.

Therefore, the present invention is to solve the problem of the catalyst is added to improve the selectivity to promote the generation of side reactions, such as green oil, the catalyst is faster deactivation and the regeneration period is short, the present invention is to add carbon monoxide and the like The present invention relates to a hydrogenation catalyst and a method for preparing a catalyst having a high selectivity without inhibiting side reactions such as polymerization or carbonylation and having a low deactivation rate and extending a continuous reaction time.

Figure 1 shows the results of the selective acetylene hydrogenation of the alpha-alumina-supported palladium catalyst on which the silicon of the present invention is chemically deposited.

Figure 2 shows the selectivity according to the temperature of the catalyst of the present invention the chemically and chemically vapor-deposited silicon.

The present invention relates to a novel catalyst and a process for selectively hydrogenating acetylene by reacting ethylene containing 0.5 to 2.0% by weight of acetylene, and the present invention also has high selectivity without addition of carbon monoxide and the like or polymerization or carbonylation. The present invention relates to a catalyst for the hydrogenation of acetylene contained in ethylene which has a slow deactivation rate by suppressing side reactions such as a reaction and has a continuous reaction time.

Therefore, in the present invention, acetylene contained in ethylene prepared by supporting 0.005 to 2.0 wt% of hydrogenation catalyst and 0.001 to 2.0 wt% of modifier of silicon on at least one carrier selected from alumina, titanium dioxide, silica, and silica alumina It relates to a catalyst composition for the hydrogenation reaction, wherein the palladium content is 0.01 to 0.2% by weight, the silicon content is preferably 0.005 to 0.2% by weight, the silicon is also used in tetrahydrosilane or triethylsilane, tripropylsilane, phenylsilane, etc. It is characterized by containing one or more selected from selected organosilane compounds.

Meanwhile, 0.03 to 2.0 wt% of a transition metal selected from nickel, cobalt, and silver may be used as a promoter, and 0.03 to 1.0 wt% of an alkali metal selected from sodium, potassium, and calcium may be included as a promoter.

In addition, in the method for preparing a catalyst of the present invention, an aqueous solution of palladium salt is impregnated with at least one carrier selected from alumina, titanium dioxide, silica, and silica alumina so as to carry 0.005 to 2.0 wt% of the catalyst palladium, followed by drying and firing at 300 to 700 ° C. After reducing under 50-500 ° C. hydrogen gas stream, 0.001 to 2.0% by weight of the silicon compound is further supported on the catalyst by chemical vapor deposition. At this time, the palladium salt is characterized in that at least one selected from palladium halide, palladium nitrate, palladium acetylacetonate, 0.03 ~ 2% by weight of the transition metal as a promoter, 0.03 ~ 1.0% by weight of the alkali metal as a catalyst palladium salt It can be supported together.

Still another object of the present invention is to provide a method for selectively hydrogenating acetylene by reacting with ethylene containing 0.5 to 2.0 wt% of acetylene using the catalyst composition of the present invention.

Hereinafter, the present invention will be described in more detail.

In addition, the catalyst of the present invention is at least one carrier selected from alumina or titanium dioxide, silica, silica alumina, the content of palladium, the hydrogenation catalyst is 0.005 to 2.0% by weight, preferably 0.01 to 0.2% by weight, 0.03 transition metal of the cocatalyst ˜2.0% by weight, 0.03 to 1.0% by weight of alkali metal as an accelerator and 0.001 to 2.0% by weight of silicon as a modifier, preferably 0.005 to 0.2% by weight. Therefore, in the present invention, a transition metal as a promoter and an alkali metal as an accelerator may be selectively added. The transition metal used may be nickel, cobalt, silver, and the like, and sodium, potassium, calcium, etc. may be used as the alkali metal. Can be used.

Palladium salts (palladium halides such as palladium chloride, palladium nitrate, palladium acetylacetonate) were used as palladium sources, and each aqueous solution was prepared and impregnated with alumina or titanium dioxide, silica, silica alumina, or the like. The impregnated catalyst was dried at room temperature to 200 ° C., preferably at 50 to 150 ° C. The dried catalyst was calcined at 300 to 700 ° C., preferably at 400 to 600 ° C., under air stream for 1 to 5 hours. Nitrogen was flowed through the calcined catalyst at room temperature to remove oxygen, and then reduced at 50 to 500 ° C., preferably at 250 to 400 ° C., for 1 to 5 hours under hydrogen stream. In the case of further supporting the promoter and the promoter, an aqueous solution of the palladium salt, the metal salt of the promoter and the promoter was prepared, impregnated into the carrier, and treated under the same conditions as the above drying and firing conditions.

Silicon was introduced to the catalyst by chemical vapor deposition using tetrahydrosilane (SiH ₄ ) or organosilane. In this case, at least one selected from triethylsilane, tripropylsilane, and phenylsilane can be used as the organosilane. After filling the catalyst prepared in a fixed bed, it was chemically deposited by flowing tetrahydrosilane or organosilane diluted in hydrogen at 100 ~ 600 ℃, preferably 300 ~ 500 ℃. 15 to 700 ° C., preferably oxidized at 15 to 100 ° C. under an air stream for 1 to 5 hours, and then reduced to 50 to 500 ° C., preferably 250 to 400 ° C. under hydrogen stream. The catalyst for acetylene hydrogenation in use can be added to the above-described silicon chemical vapor deposition step to prepare a catalyst having improved selectivity and a slow deactivation rate.

The reactants used in the catalysis experiment were ethylene containing 0.65 vol% of acetylene. The reaction hydrogen and carbon monoxide were diluted with ethylene to facilitate the concentration control. The concentrations were 8.98 vol% and 9.26 ppm, respectively, and the flow rate into the reactor was controlled by a gas flow controller. The reaction temperature is 40 to 140 ° C, preferably 60 to 100 ° C. The space velocity of the reactants is 200-2,000 (ml / min gram catalyst), preferably 400-1,000 (ml / min gram catalyst). Reactivity calculation was based on the following formula.

The catalyst prepared in the present invention showed improved results in selectivity and continuous reaction time compared to the conventional catalyst. Figure 1 shows the reaction result of each catalyst of Example 1 in the present invention. Compared to 'catalyst 1' without introducing silicon, catalysts in which silicon is introduced and deposited, in particular, 'catalyst 4', show excellent reaction results with high selectivity and yield. Figure 2 shows the change in selectivity depending on the reaction temperature of the chemically deposited catalyst of silicon of Example 1 and the catalyst not. In the case of 'catalyst 4' in which the silicon of the present invention is deposited and introduced, it exhibits higher selectivity at the same reactivity than 'catalyst 1' in which silicon is not introduced at a wide range of reaction temperatures. In addition, as shown in Table 3 of Example 1, the deactivation rate of the 'Chemical Catalyst 4' in which the silicon was chemically deposited is low, and the continuous reaction time is long.

Hereinafter, the present invention will be described in detail by way of examples. However, these Examples are only for illustrating the present invention and the present invention is not limited thereto.

Example 1

1) Catalyst Preparation

25 mg of PdCl ₃ was dissolved in 40 g of an aqueous 3% HCl solution to make a solution. 50 g of alumina (alpha form, spherical 3 mm diameter, BET surface area 60 square meters / g, average pore size 200 angstroms) was added to the solution and left for 2-3 hours and placed in a 100 ° C. oven for 4-5 hours. The dried catalyst was oxidized under air flow at 25 ° C. for 2 hours, and then flowed with nitrogen at room temperature to remove oxygen and reduced under 400 ° C. hydrogen stream. The prepared catalyst is referred to as 'catalyst 1'. 'Catalyst 1' has a composition of 0.03% by weight Pd. After filling 5 g of 'catalyst 1' into a fixed bed tube, 20 ml of 1% SiH ₄ / H ₂ gas was deposited at 400 ° C. per minute, and then fired for 2 hours under 500 ° C. air stream, and then reduced for 2 hours under 400 ° C. hydrogen stream. Catalysts were prepared with different deposition times of 5 minutes, 10 minutes, 15 minutes, 20 minutes, and 50 minutes, and are named 'catalyst 2', 'catalyst 3', 'catalyst 4', 'catalyst 5' and 'catalyst 6' for each catalyst. do. The silicon content of the catalyst is 0.0025, 0.005, 0.0075, 0.010 and 0.020% by weight, respectively.

2) Hydrogenation of Catalyst

Each 1g of the prepared catalyst was charged in a 1/2 inch stainless steel tubular reactor, and then hydrogenated under the following reaction conditions.

Reaction temperature: 100 ℃

Hydrogen / acetylene: 3/1 (molar ratio)

Reactant Space Velocity: 800 (ml / min Gram Catalyst)

The reaction results are shown in FIG. As shown in the figure, when the catalyst deposited with silicon, the conversion rate is similar and the yield is high when compared to 'catalyst 1' without the silicon deposited. In particular, 'catalyst 4' can be seen that more than three times.

3) Hydrogen / acetylene molar ratio effect

The reaction was carried out for the 'catalyst 1' and 'catalyst 4' by varying only the mole ratio of hydrogen / acetylene in Example 1 and the results are summarized in Table 1.

Table 1 Reactivity Effect of Hydrogen / acetylene Mole Ratio

As the molar ratio of hydrogen in the reactants increases, the conversion increases and the selectivity decreases. In the case of 'catalyst 1', when the hydrogen / acetylene mole ratio is 4, the selectivity has a negative value, which means that the total amount of ethylene is reduced because the ethylene hydrogenation reaction as well as the acetylene hydrogenation proceeds a lot in the reactants. In the case of 'catalyst 4', the decrease in selectivity is small even when the hydrogen / acetylene molar ratio is high, indicating that the catalyst according to the present invention effectively controls the ethylene hydrogenation reaction.

4) Carbon Monoxide Effect

The reaction was carried out for 'catalyst 1' and 'catalyst 4' by varying only the carbon monoxide concentration in the reaction conditions of Example 2 as follows and the results are summarized in Table 2.

[Table 2] Reactivity Effect of Carbon Monoxide Concentration

As the concentration of carbon monoxide increases in 'catalyst 1', the conversion rate decreases, the selectivity and the yield increase, but the selectivity and the yield are lower than the 'catalyst 4' in which the silicon is chemically deposited. The catalyst 4 according to the present invention shows high selectivity and yield compared to the existing catalyst without the injection of carbon monoxide, thereby preventing the generation of green oil and deterioration of the catalyst performance due to the injection of carbon monoxide.

5) Reaction temperature influence

The reaction was performed at different reaction temperatures for 'catalyst 1' and 'catalyst 4', and the results are shown in FIG. As the reaction temperature increases, the selectivity decreases, and when the reactivity is the same, the selectivity of 'catalyst 4' is the highest.

6) catalyst deactivation

The reaction was carried out for 30 hours under the following conditions on 'catalyst 1' and 'catalyst 4', and the deactivation rate was measured and shown in Table 3.

Reaction temperature: 120 ℃

Hydrogen / acetylene: 3/1 (molar ratio)

Reactant Space Velocity: 800 (ml / min Gram Catalyst)

[Table 3] Deactivation Rate of Catalyst

The more carbon monoxide is added, the faster the deactivation rate of the catalyst. The chemically deposited 'Catalyst 4' results in relatively slow deactivation.

As a result of the reaction under various conditions, the catalysts with chemical vapor deposition of silicon can maintain high selectivity and yield over a wide temperature range and a wide hydrogen / acetylene ratio compared to the catalysts without chemical vapor deposition, and the catalyst deactivation is slow. It can be seen.

Example 2

Instead of silane (SiH ₄ ), organosilane was used as a deposition material. A catalyst was prepared under the same conditions as in Example 1 except that the organic silane was filled with hydrogen to the liquid saturator and the organic silane was chemically deposited on 'catalyst 1'. The hydrogenation reaction was carried out under the following reaction conditions and the results are shown in Table 4.

Reaction temperature: 100 ℃

Hydrogen / acetylene: 3/1 (molar ratio)

Reactant Space Velocity: 800 (ml / min Gram Catalyst)

Table 4 Silicon Deposition Catalyst Reactivity

Regardless of the type of silane, it shows similar reactivity and the effect of supporting silicon by chemical vapor deposition is maintained.

Example 3

A catalyst was prepared in the same manner as in the method of preparing 'Catalyst 4' of Example 1, except that titanium dioxide, silica, and silica alumina were used as a carrier instead of alumina, and a hydrogenation reaction was performed under the following reaction conditions. The results are shown in Table 5.

Reaction temperature: 120 ℃

Hydrogen / acetylene: 3/1 (molar ratio)

Reactant Space Velocity: 800 (ml / min Gram Catalyst)

[Table 5] Reactivity Effect of Carrier

In the case of titanium dioxide, silica and silica alumina supported catalysts, the reactivity of the supported alumina catalysts is almost the same, meaning that the effect of supporting silicon by chemical vapor deposition is maintained regardless of the type of carrier.

Example 4

The catalyst was prepared in the same manner as the method for preparing 'catalyst 4' of Example 1, except that the cocatalyst and the promoter component were additionally supported. 5 g of 'Catalyst 1' of Example 1 was impregnated in an aqueous solution of nickel nitrate or cobalt acetate or silver (silver) nitrate in an amount to be supported and then dried. An amount of the alkali salt solution to be supported was impregnated with the dried 'catalyst 1', dried in an oven at 100 ° C., and calcined at 400 ° C. for 2 hours. After filling the calcined sample in a fixed bed tube, 20 ml of 1% SiH ₄ / H ₂ gas was poured at 400 ° C. for 20 minutes, and the catalyst was prepared by oxidation at 25 ° C. for 2 hours and reduction at 400 ° C. for 2 hours. . The hydrogenation reaction was carried out under the following reaction conditions and the results are shown in Table 6.

Reaction temperature: 120 ℃

Hydrogen / acetylene: 3/1 (molar ratio)

Reactant Space Velocity: 800 (ml / min Gram Catalyst)

[Table 6] Reactivity Effect of Cocatalysts and Accelerators

When the additional promoter and the promoter were supported, the conversion tended to increase and the selectivity was decreased. In general, the reaction result was similar to that of Example 4 'Catalyst 4'. In this case, it means that the effect of supporting silicon by chemical vapor deposition is maintained.

A catalyst having a content of 0.005 to 2.0% by weight of palladium as a hydrogenation catalyst and a content of 0.001 to 2.0% by weight of silicon as a modifier on at least one carrier selected from alumina, titanium dioxide, silica, and silica alumina, the catalyst of the present invention, is used. In the reaction of selectively hydrogenating acetylene by reacting ethylene containing 0.5 to 2.0% by weight of acetylene, the effect of the present invention has high selectivity even without addition of carbon monoxide, and suppresses side reactions such as polymerization or carbonylation. It is possible to effectively carry out the hydrogenation of acetylene contained in ethylene having a slow deactivation rate and extended continuous reaction time.

Claims (8)

Selective hydrogenation of acetylene contained in ethylene prepared by supporting 0.005 to 2.0% by weight of a hydrogenation catalyst palladium and 0.001 to 2.0% by weight of a silicone compound as a modifier on at least one carrier selected from alumina, titanium dioxide, silica, and silica alumina. Catalyst composition The catalyst composition of claim 1, wherein the palladium content is 0.01-0.2 wt% and the silicon content is 0.005-0.2 wt%. The catalyst composition of claim 1, wherein the silicon contains at least one selected from organosilane compounds selected from tetrahydrosilane or triethylsilane, tripropylsilane, phenylsilane, and the like. The method according to any one of claims 1 to 3, wherein 0.03 to 2.0 wt% of a transition metal selected from nickel, cobalt, silver, and the like is used as a promoter, and 0.03 to 1.0 wt% of an alkali metal selected from sodium, potassium, calcium, and the like is used as a promoter. Catalyst composition, characterized in that Palladium salt solution was impregnated with at least one carrier selected from alumina, titanium dioxide, silica, and silica alumina so as to support 0.005 to 2.0 wt% of the catalyst palladium, dried, calcined at 300 to 700 ° C, and then heated under 50 to 500 ° C hydrogen stream. A method for producing a catalyst composition for selectively hydrogenating acetylene contained in ethylene, wherein the ethylene is contained in the catalyst, which is reduced and further supported by 0.001 to 2.0% by weight of a silicon compound by chemical vapor deposition. The method of claim 5, wherein the palladium salt is at least one selected from palladium halide, palladium nitrate, and palladium acetylacetonate. The method for producing a catalyst composition according to claim 5 or 6, wherein 0.03 to 2% by weight of a transition metal as a promoter and 0.03 to 1.0% by weight of an alkali metal as an accelerator are supported together with a palladium salt as a catalyst. A method of selectively hydrogenating acetylene by reacting with ethylene containing 0.5 to 2.0 wt% of acetylene using the catalyst composition of claim 1