CN107774249B - Hydrogenation catalyst for producing 1, 4-diacetoxybutane - Google Patents

Abstract

The invention relates to a hydrogenation catalyst for producing 1, 4-diacetoxybutane, which mainly solves the problem of low yield and selectivity of 1, 4-diacetoxybutane in the prior art, and adopts the technical scheme that the hydrogenation catalyst for producing 1, 4-diacetoxybutane comprises a carrier and an active component, wherein the carrier is activated carbon, the active component comprises a Pt element and a cocatalyst element, and the cocatalyst element comprises at least one metal element selected from IA group metals, so that the technical problem is better solved, and the hydrogenation catalyst can be used in the industrial production of 1, 4-diacetoxybutane.

Description

Hydrogenation catalyst for producing 1, 4-diacetoxybutane

Technical Field

The present invention relates to a hydrogenation catalyst for producing 1, 4-diacetoxybutane.

Background

1,4-butanediol (1,4-BDO) is an important organic and fine chemical raw material and is widely applied to the fields of medicine, chemical industry, textile, papermaking, automobile, daily chemical industry and the like. It can derive a series of fine chemical products with high added value. For example, Tetrahydrofuran (THF), polybutylene terephthalate (PBT), gamma-butyrolactone (GBL) and polyurethane resins (PU Resin) can be produced from 1,4-BDO, and have received extensive attention from research institutes, particularly as a basic raw material for the production of PBT engineering plastics and PBT fibers.

The preparation process of 1,4-butanediol has more routes, the used raw materials include acetylene, ethylene, propylene, butadiene, maleic anhydride and other raw material routes, and the same raw materials also have different synthesis processes. Due to the high technical barriers and limited raw material sources, 1,4-BDO production is relatively centralized worldwide. In 2011, the global 1,4-BDO capacity is mainly distributed in Asia, USA and Europe, wherein the Asia 1,4-BDO capacity accounts for as high as 56.6%. At present, the industrial production method of 1,4-BDO mainly comprises the following steps: (ii) an alkynal method (Reppe method): acetylene and formaldehyde are used as raw materials, methanol copper is used as a catalyst to generate butynediol, and the butynediol is subjected to two-stage hydrogenation to obtain 1, 4-BDO. The main processes are the Reppe method developed by BASF corporation, u.s.a. DuPont and the modified Reppe method. ② a maleic anhydride method: the method takes maleic anhydride as a raw material and carries out two-step hydrogenation on the maleic anhydride. In the first step, maleic anhydride is hydrogenated to generate gamma-butyrolactone and tetrahydrofuran under the action of a Ni-Re catalyst;second step of gamma-butyrolactone in Mo-Cr-K₂Hydrogenating under the action of O catalyst to generate 1, 4-BDO. The main flow process is mainly a two-stage hydrogenation process developed by the oiling and the formation of Mitsubishi of Japan. ③ propylene method: the allyl alcohol method developed by the company of Nippon Coly at present is industrially applied, and the allyl alcohol method is used for generating 4-hydroxybutyraldehyde by liquid-phase hydroformylation of allyl alcohol under the action of a rhodium catalyst and then generating 1,4-butanediol by hydrogenation. (iv) butadiene method: the method for producing 1,4-BDO by using butadiene as a raw material mainly comprises a butadiene acetoxylation method and a butadiene chlorination method, the mainstream process of the method is developed by Mitsubishi Kabushiki Kaisha in the 80 years of the 20 th century, and the method successfully breaks the technical barrier and obstacle of the Reppe method. In particular to the advantages and the prospect of the butadiene acetoxylation method, which is favored by domestic and foreign research institutions.

As is well known, the butadiene acetoxylation method is a three-step process, namely firstly, butadiene is subjected to acetylation reaction with acetic acid and oxygen to generate 1, 4-diacetoxybutene and a byproduct of 3, 4-diacetoxybutene; then the 1, 4-diacetoxybutene is catalyzed and hydrogenated to generate the 1, 4-diene acetoxy butane, and finally hydrolysis reaction is carried out to obtain the 1, 4-BDO. In a 1, 4-butadiene to 1,4-butanediol process route in which 1, 4-diacetoxybutene is catalytically hydrogenated to 1, 4-diene acetoxybutane as one of the steps, the yield and selectivity of the hydrogenated product directly affects the yield and selectivity of 1,4-butanediol relative to 1, 4-butadiene.

U.S. Pat. No. 4032458(production of 1,4-butane diol) teaches the production of 1,4-butanediol using furan in the presence of a catalyst under certain conditions of temperature and pressure. Patent CN94108094.3 (process for preparing 1,4-butanediol) describes the preparation of 1,4-butanediol by gas phase catalytic hydrogenation reaction using maleic anhydride as raw material in the presence of a specifically designed catalyst. Patent CN104326871A (a preparation method of butanediol) describes that 2-butene with a content of more than 99% is mixed with acetic acid, nitrogen, oxygen and water vapor at a high temperature and then introduced into a fixed bed by using a fixed bed catalytic technology, and 1,4-butanediol is synthesized under the conditions of a catalyst, a certain temperature and a certain pressure, and the like. However, the methods have the problems of low yield and low selectivity of the 1,4-BDO in the process of preparing the 1, 4-BDO.

Disclosure of Invention

One of the technical problems to be solved by the invention is the problem that the yield and the selectivity of the 1, 4-diacetoxybutane are low, and the invention provides a novel hydrogenation catalyst for producing the 1, 4-diacetoxybutane, which has the characteristics of high yield and high selectivity of the 1, 4-diacetoxybutane.

The second technical problem to be solved by the invention is the preparation method of the hydrogenation catalyst.

The invention also provides a method for producing 1, 4-diacetoxybutane by using the hydrogenation catalyst.

In order to solve one of the above technical problems, the technical solution adopted by the present invention is as follows: the hydrogenation catalyst for producing the 1, 4-diacetoxybutane comprises a carrier and an active component, wherein the carrier is activated carbon, the active component comprises a Pt element and a promoter element, and the promoter element comprises at least one metal element selected from group IA metals.

In the technical scheme, the activated carbon is preferably at least one of coal columnar carbon, coconut shell activated carbon, apricot shell activated carbon and bamboo activated carbon.

In the technical scheme, the specific surface area of the activated carbon is preferably 1000-1500 cm²The preferred adsorption pore volume is 0.60-1.00 cm/g³/g。

In the above technical solution, the group IA metal in the hydrogenation catalyst is preferably at least one selected from Li, Na, K, Rb and Cs, and more preferably includes both Rb and Cs. Rb and Cs have synergistic effects in increasing the yield of 1, 4-diacetoxybutane and the selectivity of 1, 4-diacetoxybutane.

In the above technical solution, the promoter element may further comprise at least one metal element of group IIB metals, and at this time, the group IA metal element and the group IIB metal element have a synergistic effect in improving the yield of 1, 4-diacetoxybutane and the selectivity of 1, 4-diacetoxybutane in the hydrogenation reaction of 1, 4-diacetoxybutylene. By way of non-limiting example, such as but not limited to rubidium in conjunction with zinc, cesium in conjunction with zinc, and the like.

In the above technical scheme, the group IIB metal in the hydrogenation catalyst is preferably at least one of Zn, Cd and Hg. Further comprises Zn and Cd which have synergistic effect in improving the yield of 1, 4-diacetoxybutane and the selectivity of 1, 4-diacetoxybutane.

In the technical scheme, the content of Pt in the hydrogenation catalyst is preferably 0.90-8.00 g/L, and more preferably 1.50-5.00 g/L.

In the technical scheme, the content of the promoter element in the hydrogenation catalyst is preferably 0.50-10.00 g/L, and more preferably 1.00-6.00 g/L.

To solve the second technical problem, the technical solution of the present invention is as follows:

the method for preparing a hydrogenation catalyst according to any of the preceding technical solutions, comprising the steps of:

mixing a solution containing platinum elements with a carrier according to the composition of a catalyst to obtain a catalyst precursor I;

ageing the catalyst precursor I to obtain a catalyst precursor II;

reducing the combined platinum element in the catalyst precursor II into simple substance platinum to obtain a catalyst precursor III;

fourthly, washing and drying to obtain a catalyst precursor IV;

loading the compound of the promoter element on the catalyst precursor IV by adopting an impregnation method according to the composition of the catalyst, and drying to obtain the catalyst.

In the above-mentioned embodiments, as a non-limiting example, specific compounds corresponding to the platinum element in the step (i) are preferably at least one selected from the group consisting of platinum acetate, platinum chloride, ammonium chloroplatinite, dinitrosoplatinum, chloroplatinic acid, and tetraammineplatinum; more preferably ammonium platinochloride.

In the above technical solution, as a non-limiting example, the specific compound corresponding to the group IA metal element in the step (v) is preferably at least one selected from group IA metal oxides, group IA metal chlorides, group IA metal sulfates, group IA metal nitrates and group IA metal acetates; more preferably at least one group IA metal acetate; most preferably at least one selected from rubidium acetate and cesium acetate.

In the above technical solution, as a non-limiting example, when the promoter element in the fifth step includes a group IIB metal element, the specific compound corresponding to the group IIB metal element is preferably at least one selected from zinc citrate, zinc gluconate, zinc acetate, zinc nitrate, cadmium acetate, cadmium chloride, cadmium nitrate, mercury acetate, mercurous nitrate and mercury sulfate; more preferably at least one of zinc citrate and cadmium acetate.

In the above technical solution, the reducing agent in step (c) is not particularly required based on the understanding of those skilled in the art, and the reducing agent may be a gas or a liquid, and is preferably at least one of hydrogen and hydrazine hydrate; the drying temperature is preferably 30-120 ℃, and the drying time is preferably 1-5 hours; the drying temperature is preferably 80-120 ℃, and more preferably 100-120 ℃.

To solve the third technical problem, the technical scheme of the invention is as follows:

1, 4-diacetoxybutane is produced by hydrogenation of 1, 4-diacetoxybutene with hydrogen in the presence of a hydrogenation catalyst according to any one of the preceding technical claims.

The key of the invention is the selection of hydrogenation catalyst, and the skilled person knows how to determine suitable hydrogenation process conditions such as reaction temperature, reaction time, reaction pressure and feed ratio according to actual needs. However:

in the technical scheme, the temperature of the hydrogenation reaction is preferably 20-120 ℃.

In the above technical scheme, the pressure of the hydrogenation reaction is preferably 1.0-10.0 MPa, and more preferably 1.0-6.0 MPa.

In the technical scheme, the time of the hydrogenation reaction is preferably 0.5-5.0 h, and more preferably 0.5-2.0 h.

1, 4-diacetoxybutene can be obtained from commercial sources or can be produced by the butadiene oxyacetylation method. Pd-Te/C can be used as butadiene oxyacetylation catalyst in butadiene oxyacetylation method. The content of palladium element in the suitable Pd-Te/C catalyst is preferably 2.50-5.00 g/L, and more preferably 3.00-4.50 g/L; the content of tellurium is preferably 0.50 to 3.00g/L, more preferably 1.00 to 2.50 g/L. The suitable temperature of the oxyacetylation reaction is preferably 40-150 ℃; the pressure of the oxyacetylation reaction is preferably 1.0-10.0 MPa; the preferred time of the oxyacetylation reaction is 0.5-5 h; the molar ratio of butadiene to acetic acid is preferably 0.010-2.0. After the butadiene is subjected to the butadiene oxyacetylation reaction, the mixture of the butadiene oxyacetylation reaction can be separated to obtain the target product 1, 4-diacetoxybutene, and then the hydrogenation reaction is carried out, or the hydrogenation reaction can be directly carried out without separating. However, in order to eliminate other impurities to cause system complexity and facilitate the same proportion, the section of the embodiment of the invention adopts pure 1, 4-diacetyloxybutene as the hydrogenation reaction raw material.

The product mixture of the hydrogenation reaction can be separated to obtain the target product 1, 4-diacetyloxybutane.

The 1, 4-diacetoxybutane can be further used to obtain 1,4-butanediol by a hydrolysis process. The selection of an appropriate hydrolysis catalyst and the determination of an appropriate hydrolysis reaction temperature, time and feed ratio are well known to those skilled in the art. The hydrolysis catalysts which are commonly used may be inorganic acids, inorganic bases, organic acids and organic bases. Such as hydrochloric acid, nitric acid, sulfuric acid, phosphoric acid, sodium hydroxide, potassium hydroxide, benzenesulfonic acid, and ion exchange resins. The appropriate hydrolysis reaction temperature is preferably 30-100 ℃; the hydrolysis reaction pressure is preferably 0-2.0 MPa; the solvent is preferably water.

The product mixture after hydrogenation reaction is analyzed by a gas chromatography-MASS spectrometer (GC-MASS), and the yield and selectivity of 1, 4-diacetoxybutane are calculated according to the following formula:

compared with the prior art, the hydrogenation catalyst improves the yield and the selectivity of the 1, 4-diacetoxybutane.

Experimental results show that when the method is adopted, the yield of the 1, 4-diacetyloxy butane is over 82 percent, the selectivity is over 94 percent, and a better technical effect is achieved. Particularly, when the active component of the hydrogenation catalyst simultaneously comprises platinum, at least one metal element selected from group IA metals and at least one metal element selected from group IIB metals, more remarkable technical effects are obtained. The invention is further illustrated by the following examples.

Detailed Description

[ example 1 ]

Preparation of hydrogenation catalyst:

[ solution ] ammonium chloroplatinite ((NH) containing 2.05g of Pt₄)₂PtCl₄) Dissolving in 8 wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm, and pore volume of 0.80cm³A specific surface area of 1200 cm/g²Soaking a coal cylindrical active carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

fourthly, washing the solution until no chloride ion exists, and drying the solution for 4 hours at 50 ℃ to obtain a catalyst precursor IV;

immersing 180ml of aqueous solution of 2.10g Rb-containing rubidium acetate (RbOAc) on the catalyst precursor IV, and drying at 110 ℃ for 4 hours to obtain the catalyst.

The Pt content of the catalyst was determined by ICP to be 2.05g/L and the Rb content was determined to be 2.10 g/L.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 1.0MPa, introducing hydrogen until the pressure is 3.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 60 ℃, continuously reacting for 90min, and stopping the reaction.

The yield of 1, 4-diacetoxybutane was analytically calculated to be 82.25% and the selectivity 94.27%, and for convenience of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the yield of 1, 4-diacetoxybutane and the selectivity are shown in tables 1 and 2, respectively.

[ example 2 ]

Preparation of hydrogenation catalyst:

[ solution ] ammonium chloroplatinite ((NH) containing 2.05g of Pt₄)₂PtCl₄) Dissolving in 8 wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm, and pore volume of 0.80cm³A specific surface area of 1200 cm/g²Soaking a coal cylindrical active carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

fourthly, washing the solution until no chloride ion exists, and drying the solution for 4 hours at 50 ℃ to obtain a catalyst precursor IV;

fifthly, zinc citrate (Zn) containing 2.10g Zn₃(C₆H₅O₇)₂·2H₂O) was impregnated on the catalyst precursor IV in 180ml of an aqueous solution and dried at 110 ℃ for 4 hours to obtain the catalyst.

The Pt content of the catalyst was determined by ICP to be 2.05g/L and the Zn content was determined to be 2.10 g/L.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 1.0MPa, introducing hydrogen until the pressure is 3.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 60 ℃, continuously reacting for 90min, and stopping the reaction.

The yield of 1, 4-diacetoxybutane was calculated analytically to be 82.72% and the selectivity was 93.87%, and for ease of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amounts, the yield of 1, 4-diacetoxybutane and the selectivity were shown in tables 1 and 2, respectively.

[ COMPARATIVE EXAMPLE 1 ]

Are comparative examples of [ example 1 ] and [ example 2 ].

Preparation of hydrogenation catalyst:

[ solution ] ammonium chloroplatinite ((NH) containing 2.05g of Pt₄)₂PtCl₄) Dissolving in 8 wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm, and pore volume of 0.80cm³A specific surface area of 1200 cm/g²Soaking a coal cylindrical active carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

and fourthly, washing the catalyst with water until no chloride ion exists, and drying the catalyst for 4 hours at 50 ℃ to obtain the catalyst.

The Pt content of the catalyst was determined by ICP to be 2.05 g/L.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 1.0MPa, introducing hydrogen until the pressure is 3.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 60 ℃, continuously reacting for 90min, and stopping the reaction.

The yield of 1, 4-diacetoxybutane was calculated analytically to be 75.10% and the selectivity was 91.59%, and for ease of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amounts, the yield of 1, 4-diacetoxybutane and the selectivity were shown in tables 1 and 2, respectively.

Compared with the examples 1-2, the catalyst adopting hydrogenation has the advantages that the catalyst containing Pt and Rb as active components and Pt and Zn as active components has better performance than the catalyst containing Pt as active components, and the catalyst containing Pt and Zn as active components is favorable for improving the activity and stability of the hydrogenation catalyst and has high yield and selectivity of 1, 4-diacetoxybutane.

[ COMPARATIVE EXAMPLE 2 ]

Comparative example [ comparative example 1 ].

Preparation of hydrogenation catalyst:

[ solution ] ammonium chloropalladite ((NH) containing 2.05g of Pd₄)₂PdCl₄) Dissolving in 8 wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm, and pore volume of 0.80cm³A specific surface area of 1200 cm/g²Soaking a coal cylindrical active carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

and fourthly, washing the catalyst with water until no chloride ion exists, and drying the catalyst for 4 hours at 50 ℃ to obtain the catalyst.

The Pd content of the catalyst was determined by ICP to be 2.05 g/L.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 1.0MPa, introducing hydrogen until the pressure is 3.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 60 ℃, continuously reacting for 90min, and stopping the reaction.

The yield of 1, 4-diacetoxybutane was calculated analytically to be 70.05% and the selectivity was 88.16%, and for ease of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amounts, the yield of 1, 4-diacetoxybutane and the selectivity were shown in tables 1 and 2, respectively.

Compared with the comparative example 1, the catalyst adopting hydrogenation has better performance than the catalyst containing Pd active component, which shows that the hydrogenation catalyst uses Pt as the active component to favor the hydrogenation of 1, 4-diacetoxybutene and the yield and the selectivity of 1, 4-diacetoxybutane are high.

[ example 3 ]

Preparation of hydrogenation catalyst:

[ solution ] ammonium chloroplatinite ((NH) containing 2.05g of Pt₄)₂PtCl₄) Dissolving in 8 wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm, and pore volume of 0.80cm³A specific surface area of 1200 cm/g²Soaking a coal cylindrical active carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

fourthly, washing the solution until no chloride ion exists, and drying the solution for 4 hours at 50 ℃ to obtain a catalyst precursor IV;

fifthly, cadmium acetate (Cd (OA) containing 2.10g Cd_C)₂·2H₂O) was dissolved in an aqueous solution of acetic acid having a concentration of 10% by weight to obtain 180ml of an impregnation solution, which was impregnated on the catalyst precursor IV and dried at 110 ℃ for 4 hours to obtain the catalyst.

The Pt content of the catalyst is 2.05g/L and the Cd content is 2.10g/L through ICP determination.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 1.0MPa, introducing hydrogen until the pressure is 3.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 60 ℃, continuously reacting for 90min, and stopping the reaction.

The yield of 1, 4-diacetoxybutane was calculated analytically to be 82.65% and the selectivity 93.58%, and for ease of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed rates, the yield of 1, 4-diacetoxybutane and the selectivity were shown in tables 1 and 2, respectively.

[ example 4 ]

Preparation of hydrogenation catalyst:

[ solution ] ammonium chloroplatinite ((NH) containing 2.05g of Pt₄)₂PtCl₄) Dissolving in 8 wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm, and pore volume of 0.60cm³Per g, specific surface area 1000cm²Soaking a coconut shell cylindrical activated carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

fourthly, washing the solution until no chloride ion exists, and drying the solution for 4 hours at 50 ℃ to obtain a catalyst precursor IV;

fifthly, soaking 180ml of lithium acetate (LiOAc) water solution containing 2.10g of Li on the catalyst precursor IV, and drying for 4 hours at 100 ℃ to obtain the catalyst.

The Pt content of the catalyst was determined by ICP to be 2.05g/L and the Li content was determined to be 2.10 g/L.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 1.0MPa, introducing hydrogen until the pressure is 3.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 60 ℃, continuously reacting for 90min, and stopping the reaction.

The yield of 1, 4-diacetoxybutane was found to be 82.41% by analysis, and the selectivity was found to be 94.16%, and for convenience of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the yield of 1, 4-diacetoxybutane and the selectivity were shown in tables 1 and 2, respectively.

[ example 5 ]

Preparation of hydrogenation catalyst:

[ solution ] ammonium chloroplatinite ((NH) containing 2.05g of Pt₄)₂PtCl₄) Dissolving in 8 wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm and pore volume of 1.00cm³Per g, specific surface area 1500cm²Soaking the apricot shell cylindrical active carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

fourthly, washing the solution until no chloride ion exists, and drying the solution for 4 hours at 50 ℃ to obtain a catalyst precursor IV;

fifthly, soaking 180ml of sodium acetate (NaOAc) water solution containing 2.10g of Na on the catalyst precursor IV, and drying for 4 hours at 120 ℃ to obtain the catalyst.

The catalyst had a Pt content of 2.05g/L and a Na content of 2.10g/L as determined by ICP.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 1.0MPa, introducing hydrogen until the pressure is 3.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 60 ℃, continuously reacting for 90min, and stopping the reaction.

The yield of 1, 4-diacetoxybutane was found to be 82.13% by analysis, and the selectivity was found to be 94.24%, and for ease of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed rates, and the yield and selectivity of 1, 4-diacetoxybutane are shown in tables 1 and 2, respectively.

[ example 6 ]

Preparation of hydrogenation catalyst:

[ solution ] ammonium chloroplatinite ((NH) containing 2.05g of Pt₄)₂PtCl₄) Dissolving in 8 wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm, and pore volume of 0.80cm³A specific surface area of 1200 cm/g²Soaking a bamboo cylindrical activated carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

fourthly, washing the solution until no chloride ion exists, and drying the solution for 4 hours at 50 ℃ to obtain a catalyst precursor IV;

fifthly, soaking 180ml of potassium acetate (KOAc) water solution containing 2.10g K on the catalyst precursor IV, and drying for 4 hours at 110 ℃ to obtain the catalyst.

The Pt content of the catalyst was determined by ICP to be 2.05g/L and the K content was determined to be 2.10 g/L.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 1.0MPa, introducing hydrogen until the pressure is 3.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 60 ℃, continuously reacting for 90min, and stopping the reaction.

The yield of 1, 4-diacetoxybutane was calculated analytically to be 82.11% and the selectivity was 94.28%, and for ease of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amounts, the yield of 1, 4-diacetoxybutane and the selectivity were shown in tables 1 and 2, respectively.

[ example 7 ]

Preparation of hydrogenation catalyst:

[ solution ] ammonium chloroplatinite ((NH) containing 2.05g of Pt₄)₂PtCl₄) Dissolving in 8 wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm, and pore volume of 0.80cm³A specific surface area of 1200 cm/g²Soaking a coal cylindrical active carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

fourthly, washing the solution until no chloride ion exists, and drying the solution for 4 hours at 50 ℃ to obtain a catalyst precursor IV;

fifthly, soaking 180ml of aqueous solution of cesium acetate (CsOAc) containing 2.10g Cs on the catalyst precursor IV, and drying at 110 ℃ for 4 hours to obtain the catalyst.

The Pt content of the catalyst was determined by ICP to be 2.05g/L and the Cs content was determined to be 2.10 g/L.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 1.0MPa, introducing hydrogen until the pressure is 3.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 50 ℃, continuously reacting for 90min, and stopping the reaction.

The yield of 1, 4-diacetoxybutane was found to be 82.17% by analysis, and the selectivity was found to be 94.25%, and for convenience of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the yield of 1, 4-diacetoxybutane and the selectivity were shown in tables 1 and 2, respectively.

[ example 8 ]

Preparation of hydrogenation catalyst:

[ solution ] ammonium chloroplatinite ((NH) containing 1.50g of Pt₄)₂PtCl₄) Dissolved at a concentration of 8wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm, and pore volume of 0.80cm³A specific surface area of 1200 cm/g²Soaking a coal cylindrical active carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

fourthly, washing the solution until no chloride ion exists, and drying the solution for 4 hours at 50 ℃ to obtain a catalyst precursor IV;

fifthly, soaking 180ml of cesium acetate (CsOAc) water solution containing 1.00g of Cs on the catalyst precursor IV, and drying at 110 ℃ for 4 hours to obtain the catalyst.

The Pt content of the catalyst was 1.50g/L and the Cs content was 1.00g/L as determined by ICP.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 0.5MPa, introducing hydrogen until the pressure is 1.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 20 ℃, continuously reacting for 30min, and stopping the reaction. Cooling the reaction kettle to room temperature, and purifying to remove impurities to obtain the 1, 4-diacetyloxy butane.

The yield of 1, 4-diacetoxybutane was analytically calculated to be 80.85% and the selectivity 94.05%, and for convenience of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the yield of 1, 4-diacetoxybutane and the selectivity are shown in tables 1 and 2, respectively.

[ example 9 ]

Preparation of hydrogenation catalyst:

(ii) ammonium platinochloride ((NH) containing 5.00g of Pt)₄)₂PtCl₄) Dissolving in 8 wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm, and pore volume of 0.80cm³A specific surface area of 1200 cm/g²Soaking a coal cylindrical active carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

fourthly, washing the solution until no chloride ion exists, and drying the solution for 4 hours at 50 ℃ to obtain a catalyst precursor IV;

fifthly, soaking 180ml of cesium acetate (CsOAc) water solution containing 6.00g of Cs on the catalyst precursor IV, and drying at 110 ℃ for 4 hours to obtain the catalyst.

The Pt content of the catalyst was determined by ICP to be 5.00g/L and the Cs content was determined to be 6.00 g/L.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 1.0MPa, introducing hydrogen until the pressure is 6.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 120 ℃, continuously reacting for 120min, and stopping the reaction.

The yield of 1, 4-diacetoxybutane was calculated analytically to be 82.48% and the selectivity was 93.89%, and for ease of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amounts, the yield of 1, 4-diacetoxybutane and the selectivity were shown in tables 1 and 2, respectively.

[ example 10 ]

Preparation of hydrogenation catalyst:

[ solution ] ammonium chloroplatinite ((NH) containing 2.05g of Pt₄)₂PtCl₄) Dissolving in 8 wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm, and pore volume of 0.80cm³A specific surface area of 1200 cm/g²Soaking a coal cylindrical active carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

fourthly, washing the solution until no chloride ion exists, and drying the solution for 4 hours at 50 ℃ to obtain a catalyst precursor IV;

fifthly, soaking 180ml of aqueous solution of rubidium acetate (RbOAc) and cesium acetate (CsOAc) containing 0.84g of Rb and 1.26g of Cs on the catalyst precursor IV, and drying at 110 ℃ for 4 hours to obtain the catalyst.

The Pt content of the catalyst is 2.05g/L, the Rb content is 0.84g/L and the Cs content is 1.26g/L through ICP determination.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 1.0MPa, introducing hydrogen until the pressure is 3.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 60 ℃, continuously reacting for 90min, and stopping the reaction.

The yield of 1, 4-diacetoxybutane was found to be 83.05% by analysis and the selectivity to 94.52%, and for convenience of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the yield of 1, 4-diacetoxybutane and the selectivity to 1, 4-diacetoxybutane were shown in tables 1 and 2, respectively.

From example 10 in comparison with examples 1 and 7, it can be seen that the metal element Rb and the metal element Cs in the group IA metals in the hydrogenation catalyst used in the present invention have a better synergistic effect in increasing the yield and selectivity of 1, 4-diacetoxybutane.

[ example 11 ]

Preparation of hydrogenation catalyst:

[ solution ] ammonium chloroplatinite ((NH) containing 2.05g of Pt₄)₂PtCl₄) Dissolving in 8 wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm, and pore volume of 0.80cm³A specific surface area of 1200 cm/g²Soaking a coal cylindrical active carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

fourthly, washing the solution until no chloride ion exists, and drying the solution for 4 hours at 50 ℃ to obtain a catalyst precursor IV;

fifthly, zinc citrate (Zn) containing 0.78g Zn and 1.32g Cd₃(C₆H₅O₇)₂·2H₂O) and cadmium acetate (Cd (OA)_C)₂·2H₂O) was impregnated on the catalyst precursor IV in 180ml of an aqueous solution and dried at 110 ℃ for 4 hours to obtain the catalyst.

The catalyst has Pt content of 2.05g/L, Zn content of 0.78g/L and Cd content of 1.32g/L as determined by ICP.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 1.0MPa, introducing hydrogen until the pressure is 3.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 60 ℃, continuously reacting for 90min, and stopping the reaction.

The yield of 1, 4-diacetoxybutane was found to be 83.71% by analysis and the selectivity to 94.38%, and for ease of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed rates, the yield of 1, 4-diacetoxybutane and the selectivity to 1, 4-diacetoxybutane were shown in tables 1 and 2, respectively.

As can be seen from the comparison between example 11 and examples 2 and 3, in the hydrogenation catalyst used in the present invention, the metal element Zn and the metal element Cd in the group IIB metal have a good synergistic effect in increasing the yield and selectivity of 1, 4-diacetoxybutane.

[ example 12 ]

Preparation of hydrogenation catalyst:

[ solution ] ammonium chloroplatinite ((NH) containing 2.05g of Pt₄)₂PtCl₄) Dissolving in 8 wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm, and pore volume of 0.80cm³A specific surface area of 1200 cm/g²Soaking a coal cylindrical active carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

fourthly, washing the solution until no chloride ion exists, and drying the solution for 4 hours at 50 ℃ to obtain a catalyst precursor IV;

fifthly, rubidium acetate (RbOAc) containing 0.83g of Rb and 1.27g of Zn and zinc citrate (Zn)₃(C₆H₅O₇)₂·2H₂O) 180ml of an aqueous solution, was impregnated on the catalyst precursor IV, and dried at 110 ℃ for 4 hours to obtain the catalyst.

The catalyst has a Pt content of 2.05g/L, an Rb content of 0.83g/L and a Zn content of 1.27g/L as determined by ICP.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 1.0MPa, introducing hydrogen until the pressure is 3.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 60 ℃, continuously reacting for 90min, and stopping the reaction.

The yield of 1, 4-diacetoxybutane was found to be 84.72% by analysis and the selectivity was found to be 95.11%, and for convenience of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the yield of 1, 4-diacetoxybutane and the selectivity were shown in tables 1 and 2, respectively.

As can be seen from example 12 in comparison with examples 1 and 2, the hydrogenation catalyst used in the present invention has a better synergistic effect of Rb, a metal element in the IA group metal, and Zn, a metal element in the IIB group metal, in increasing the yield and selectivity of 1, 4-diacetoxybutane.

[ example 13 ]

Preparation of hydrogenation catalyst:

[ solution ] ammonium chloroplatinite ((NH) containing 2.05g of Pt₄)₂PtCl₄) Dissolving in 8 wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm, and pore volume of 0.80cm³A specific surface area of 1200 cm/g²Soaking a coal cylindrical active carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

fourthly, washing the solution until no chloride ion exists, and drying the solution for 4 hours at 50 ℃ to obtain a catalyst precursor IV;

fifthly, adding cesium acetate (CsOAc) and zinc citrate (Zn) with 0.83g of Cs and 1.27g of Zn₃(C₆H₅O₇)₂·2H₂O) 180ml of an aqueous solution, was impregnated on the catalyst precursor IV, and dried at 110 ℃ for 4 hours to obtain the catalyst.

The catalyst has a Pt content of 2.05g/L, a Cs content of 0.83g/L and a Zn content of 1.27g/L as determined by ICP.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 1.0MPa, introducing hydrogen until the pressure is 3.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 60 ℃, continuously reacting for 90min, and stopping the reaction.

The yield of 1, 4-diacetoxybutane was calculated analytically to be 84.81% and the selectivity was 95.04%, and for ease of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amounts, the yield of 1, 4-diacetoxybutane and the selectivity were shown in tables 1 and 2, respectively.

From example 13, which is comparable to example 2 and example 7, it can be seen that the hydrogenation catalyst used in the present invention has a better synergistic effect of the metal element Cs in the group IA metal and the metal element Zn in the group IIB metal in terms of increasing the yield and selectivity of 1, 4-diacetoxybutane.

[ example 14 ]

Preparation of hydrogenation catalyst:

[ solution ] ammonium chloroplatinite ((NH) containing 2.05g of Pt₄)₂PtCl₄) Dissolving in 8 wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm, and pore volume of 0.80cm³A specific surface area of 1200 cm/g²Soaking a coal cylindrical active carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

fourthly, washing the solution until no chloride ion exists, and drying the solution for 4 hours at 50 ℃ to obtain a catalyst precursor IV;

fifthly, 0.33g Rb, 0.50g Cs and 1.27g Zn in rubidium acetate (RbOAc), cesium acetate (CsOAc) and zinc citrate (Zn)₃(C₆H₅O₇)₂·2H₂O) 180ml of an aqueous solution, was impregnated on the catalyst precursor IV, and dried at 110 ℃ for 4 hours to obtain the catalyst.

The catalyst has Pt content of 2.05g/L, Rb content of 0.33g/L, Cs content of 0.50g/L and Zn content of 1.27g/L through ICP determination.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 1.0MPa, introducing hydrogen until the pressure is 3.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 60 ℃, continuously reacting for 90min, and stopping the reaction.

The yield of 1, 4-diacetoxybutane was found to be 85.27% by analysis, and the selectivity was found to be 95.56%, and for convenience of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the yield of 1, 4-diacetoxybutane and the selectivity were shown in tables 1 and 2, respectively.

As can be seen from the comparison between example 14 and examples 12 and 13, the hydrogenation catalyst used in the present invention has a better synergistic effect of the metal elements Rb, Cs and Zn in the group IA metals in terms of increasing the yield and selectivity of 1, 4-diacetoxybutane.

[ example 15 ]

Preparation of hydrogenation catalyst:

[ solution ] ammonium chloroplatinite ((NH) containing 2.05g of Pt₄)₂PtCl₄) Dissolving in 8 wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm, and pore volume of 0.80cm³A specific surface area of 1200 cm/g²Soaking a coal cylindrical active carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

fourthly, washing the solution until no chloride ion exists, and drying the solution for 4 hours at 50 ℃ to obtain a catalyst precursor IV;

fifthly, rubidium acetate (RbOAc) containing 0.33g Rb, 0.50g Cs and 1.27g Cd, cesium acetate (CsOAc) and cadmium acetate (Cd (OA)_C)₂·2H₂O) was dissolved in an aqueous solution of acetic acid having a concentration of 10% by weight to obtain 180ml of an impregnation solution, which was impregnated on the catalyst precursor IV and dried at 110 ℃ for 4 hours to obtain the catalyst.

The catalyst has Pt content of 2.05g/L, Rb content of 0.33g/L, Cs content of 0.50g/L and Cd content of 1.27g/L determined by ICP.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 1.0MPa, introducing hydrogen until the pressure is 3.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 60 ℃, continuously reacting for 90min, and stopping the reaction.

The yield of 1, 4-diacetoxybutane was found to be 85.38% by analysis, and the selectivity was found to be 95.47%, and for convenience of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the yield of 1, 4-diacetoxybutane and the selectivity were shown in tables 1 and 2, respectively.

[ example 16 ]

Preparation of hydrogenation catalyst:

[ solution ] ammonium chloroplatinite ((NH) containing 2.05g of Pt₄)₂PtCl₄) Dissolving in 8 wt% hydrochloric acid aqueous solution to obtain 200ml of impregnation solution, and mixing 1L of solution with diameter of 3mm, length of 2cm, and pore volume of 0.80cm³A specific surface area of 1200 cm/g²Soaking a coal cylindrical active carbon carrier in the soaking solution to obtain a catalyst precursor I;

② standing and aging for 24h to obtain a catalyst precursor II;

③ using 8 percent of N₂H₄·H₂O weight ratio) of 500ml of hydrazine hydrate is used for reducing the catalyst precursor II for 3h to obtain a catalyst precursor III;

fourthly, washing the solution until no chloride ion exists, and drying the solution for 4 hours at 50 ℃ to obtain a catalyst precursor IV;

fifthly, rubidium acetate (RbOAc), cesium acetate (CsOAc) and zinc citrate (Zn) with 0.33g of Rb, 0.50g of Cs, 0.47g of Zn and 0.80g of Cd₃(C₆H₅O₇)₂·2H₂O) and cadmium acetate (Cd (OA)_C)₂·2H₂O) was dissolved in an aqueous solution of acetic acid having a concentration of 10% by weight to obtain 180ml of an impregnation solution, which was impregnated on the catalyst precursor IV and dried at 110 ℃ for 4 hours to obtain the catalyst.

The catalyst has Pt content of 2.05g/L, Rb content of 0.33g/L, Cs content of 0.50g/L, Zn content of 0.47g/L and Cd content of 0.80g/L determined by ICP.

Production of 1, 4-diacetoxybutane:

adding 15ml of 1, 4-diacetoxybutene, 30ml of toluene and 0.01mol of hydrogenation catalyst into a 100ml titanium reaction kettle, discharging air in the kettle by using argon, pressurizing to 1.0MPa, introducing hydrogen until the pressure is 3.0MPa, increasing the stirring speed to 600rpm, stirring, heating to the reaction temperature, controlling the reaction temperature to be 60 ℃, continuously reacting for 90min, and stopping the reaction.

The yield of 1, 4-diacetoxybutane was analytically calculated to be 86.75% and the selectivity 95.83%, and for convenience of illustration and comparison, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the yield of 1, 4-diacetoxybutane and the selectivity are shown in tables 1 and 2, respectively.

As can be seen from the comparison between example 16 and examples 14 and 15, the hydrogenation catalyst used in the present invention has a better synergistic effect of metal elements Rb, Cs in group IA metals and Zn and Cd in group IIB metals in terms of improving the yield and selectivity of 1, 4-diacetoxybutane.

TABLE 1

TABLE 2

Claims (9)

1. The hydrogenation catalyst for producing the 1, 4-diacetoxybutane comprises a carrier and an active component, wherein the carrier is activated carbon, the active component comprises a Pt element and a cocatalyst element, the cocatalyst element comprises a group IA metal, the group IA metal is Rb and Cs, the content of the Pt element in the hydrogenation catalyst is 0.90 ~ 8.00.00 g/L, and the content of the cocatalyst element in the hydrogenation catalyst is 0.50 ~ 10.00.00 g/L.

2. The hydrogenation catalyst according to claim 1, wherein the activated carbon is at least one of coal columnar carbon, coconut shell activated carbon, apricot shell activated carbon, and bamboo activated carbon.

3. Hydrogenation catalyst according to claim 1, characterized in that the activated carbon has a specific surface area of 1000 ~ 1500 m²Per g, the adsorption pore volume is 0.60 ~ 1.00.00 cm³/g。

4. A process for preparing a hydrogenation catalyst as claimed in claim 1, comprising the steps of:

mixing a solution containing platinum elements with a carrier according to the composition of a catalyst to obtain a catalyst precursor I;

ageing the catalyst precursor I to obtain a catalyst precursor II;

reducing the combined platinum element in the catalyst precursor II into simple substance platinum to obtain a catalyst precursor III;

fourthly, washing and drying to obtain a catalyst precursor IV;

loading promoter element solution on the catalyst precursor IV by adopting an immersion method according to the composition of the catalyst, and drying to obtain the catalyst.

A process for producing 1, 4-diacetoxybutane, which comprises subjecting 1, 4-diacetoxybutene to hydrogenation reaction with hydrogen in the presence of a hydrogenation catalyst to obtain 1, 4-diacetoxybutane,

the hydrogenation catalyst comprises a carrier and an active component, wherein the carrier is activated carbon, the active component comprises Pt element and a promoter element, the promoter element comprises at least one metal element selected from IA group metals,

the hydrogenation catalyst is characterized in that the IA group metal is at least one selected from Li, Na, K, Rb and Cs, the content of Pt element in the hydrogenation catalyst is 0.90 ~ 8.00.00 g/L, and the content of promoter element in the hydrogenation catalyst is 0.50 ~ 10.00.00 g/L.

6. The production method according to claim 5, characterized in that the activated carbon is at least one of coal columnar carbon, coconut shell activated carbon, apricot shell activated carbon, and bamboo activated carbon.

7. The production method according to claim 5, characterized in that the specific surface area of the activated carbon is 1000 ~ 1500 m²Per g, the adsorption pore volume is 0.60 ~ 1.00.00 cm³/g。

8. The production process according to claim 5, wherein the hydrogenation reaction is carried out at a temperature of 20 to 120 ℃.

9. The production process as claimed in claim 5, wherein the pressure of the hydrogenation reaction is 1.0 ~ 10.0.0 MPa.