Method for synthesizing 1, 3-butadiene through continuous catalytic conversion of acetylene

Abstract

The invention provides a method for synthesizing 1, 3-butadiene by continuous catalytic conversion of acetylene, which comprises the following steps: S1, continuously introducing acetylene as a raw material into a reactor I for acetylene dimerization catalytic reaction to obtain primary reaction gas containing vinyl acetylene; and S2, continuously introducing the initial reaction gas and hydrogen into a reactor II, and carrying out selective catalytic hydrogenation reaction to obtain 1, 3-butadiene. The technical scheme of the invention provides a continuous catalytic process method, and 1, 3-butadiene is directly synthesized by using acetylene as a raw material through coupling acetylene catalytic dimerization reaction and vinyl acetylene selective catalytic hydrogenation reaction. The obtained product is easy to separate from a catalytic system, and the whole process flow is simple to operate, economical and environment-friendly, and has a good application prospect.

Description

Technical Field

[0001] The present invention relates to the technical field of petrochemical industry, and in particular, to a method for continuously catalytically converting acetylene to synthesize 1,3-butadiene. Background Art

[0002] As an important organic chemical raw material, 1,3-butadiene can further undergo polymerization, substitution, addition, cyclization and other reactions, so it is often used as a key raw material for the production of cis-butadiene rubber, styrene-butadiene rubber, etc. It can also undergo olefin hydrocyanation to synthesize adiponitrile, and further hydrogenation to synthesize hexamethylenediamine and polymerization to synthesize nylon 66. At present, 1,3-butadiene is mainly produced by two processes: catalytic dehydrogenation of C4 alkanes and C4 olefins, and C4 extraction from ethylene cracking by-products. In view of the irreplaceable and wide uses of 1,3-butadiene, it is of great significance to increase its production capacity and develop new production methods.

[0003] Acetylene, as a key gas for metal welding and cutting, can be produced by the carbide method and the natural gas method. Since natural gas resources in China are relatively rich, the use of the natural gas method to produce acetylene can significantly increase the production capacity of acetylene. Therefore, under this background, using acetylene as a raw material and realizing its conversion and synthesis of 1,3-butadiene through process design is a feasible idea to increase the production capacity of 1,3-butadiene at present.

[0004] Based on this, in view of the market demand for 1,3-butadiene and the market prospects and technical bottlenecks faced by the existing catalytic dimerization of acetylene to synthesize vinylacetylene and selective catalytic hydrogenation of vinylacetylene to synthesize 1,3-butadiene, how to develop a method for continuously catalytically converting acetylene to synthesize 1,3-butadiene, and at the same time making it have a high acetylene conversion rate and 1,3-butadiene selectivity is one of the problems to be solved in this field. Summary of the Invention

[0005] The main object of the present invention is to provide a method for continuously catalytically converting acetylene to synthesize 1,3-butadiene, so as to solve the problem that it is difficult to directly synthesize 1,3-butadiene with high conversion rate and high 1,3-butadiene selectivity using acetylene as a raw material in the prior art.

[0006] To achieve the above object, the present invention provides a method for continuously catalytically converting acetylene to synthesize 1,3-butadiene, including: Step S1, using acetylene as a raw material and continuously introducing it into reactor I for acetylene dimerization catalytic reaction to obtain a primary reaction gas, wherein the primary reaction gas includes vinylacetylene; Step S2, continuously introducing the primary reaction gas and hydrogen into reactor II for selective catalytic hydrogenation reaction to obtain 1,3-butadiene.

[0007] Furthermore, in the selective catalytic hydrogenation reaction in step S2, PdM / α-Al2O3 is used as the catalyst, and the M element is one or more of Zn, Co, Ni, and Cu; preferably, in the PdM / α-Al2O3 catalyst, the mass loading of PdM is 0.1-0.5%; preferably, in the PdM / α-Al2O3 catalyst, the mass ratio of Pd to the M element is (1-5):5.

[0008] Furthermore, the PdM / α-Al2O3 catalyst is synthesized by the following steps: (1) Pd(OAc)2 and the nitrate of the M element are added to an aqueous solution containing α-Al2O3, stirred, impregnated, adsorbed, and then the water is removed to obtain a solid powder; (2) the solid powder is subjected to a reduction reaction to obtain the PdM / α-Al2O3 catalyst.

[0009] Furthermore, in step (2), the temperature of the reduction reaction is 200-400°C, and the reduction atmosphere is a H2 / Ar stream, preferably the volume ratio of H2 to Ar is 1:(2-4).

[0010] Furthermore, in the selective catalytic hydrogenation reaction in step S2, the volume ratio of the initial reaction gas to hydrogen is (80-100):(15-30); preferably, the selective catalytic hydrogenation reaction is carried out at room temperature.

[0011] Furthermore, in step S1, acetylene is introduced into reactor I in the form of an acetylene / nitrogen mixture, and the volume content of acetylene in the acetylene / nitrogen mixture is 15-30%.

[0012] Furthermore, acetylene is continuously introduced into a reaction solution including water, cuprous chloride, ammonium chloride, and hydrogen chloride for the acetylene dimerization catalytic reaction.

[0013] Furthermore, hydrogen chloride is added in the form of a hydrochloric acid solution, and the concentration of the hydrochloric acid solution is 2-5 mol / L; preferably, the weight ratio of cuprous chloride to ammonium chloride in the reaction solution is (20-40):(15-40); preferably, the volume ratio of the hydrochloric acid solution to the reaction solution for the acetylene dimerization catalytic reaction is (2-5):(50-100); preferably, the mass concentration of cuprous chloride in the reaction solution is 23-25%.

[0014] Furthermore, the reaction temperature in reactor I is 80-100°C, preferably 90-95°C.

[0015] Furthermore, in step S1, the yield of vinylacetylene is 70-77%; in step S2, the conversion rate of the selective catalytic hydrogenation reaction is 72-98%, and the selectivity of 1,3-butadiene > 62%.

[0016] Applying the technical solution of the present invention, coupling the catalytic dimerization reaction of acetylene and the selective catalytic hydrogenation reaction of vinylacetylene, a continuous catalytic process method is provided to directly synthesize 1,3-butadiene from acetylene as the raw material. The obtained product is easy to be separated from the catalytic system, the whole process flow is simple to operate, economical and environmentally friendly, and has good application prospects. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] The accompanying drawings forming a part of this application are used to provide a further understanding of the present invention. The schematic embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation to the present invention. In the drawings:

[0018] Figure 1 It is a schematic diagram of the synthesis route of the method for continuously catalytically converting acetylene to synthesize 1,3-butadiene provided by the present invention;

[0019] Figure 2 It is a transmission electron microscope image of the PdCu / α-Al2O3 catalyst prepared by the present invention. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0020] It should be noted that, without conflict, the embodiments in this application and the features in the embodiments can be combined with each other. The present invention will be described in detail below with reference to the embodiments.

[0021] As described in the background art, it is difficult to directly synthesize 1,3-butadiene from acetylene as the raw material with high conversion rate and high 1,3-butadiene selectivity. To solve the above technical problems, the present application provides a method for continuously catalytically converting acetylene to synthesize 1,3-butadiene, including: Step S1, using acetylene as the raw material, continuously introducing it into Reactor I for the catalytic dimerization reaction of acetylene to obtain a primary reaction gas, and the primary reaction gas includes vinylacetylene; Step S2, continuously introducing the primary reaction gas and hydrogen into Reactor II for the selective catalytic hydrogenation reaction to obtain 1,3-butadiene.

[0022] The continuous catalytic method provided by the present invention realizes the direct synthesis of 1,3-butadiene from acetylene by coupling the acetylene catalytic dimerization reaction and the selective catalytic hydrogenation reaction of vinylacetylene. The involved process flow is simple, and the products of each step are easy to be separated and obtained. Specifically, in step S1, acetylene is used as a raw material for the acetylene dimerization catalytic reaction to obtain a primary reaction gas containing vinylacetylene, and the yield of vinylacetylene can reach up to 77%; the obtained primary reaction gas is directly subjected to a selective catalytic hydrogenation reaction with hydrogen without any treatment to obtain 1,3-butadiene, and the selectivity of 1,3-butadiene in the hydrogenation reaction can reach up to 98%. Thus, under the conditions of simplifying the process flow, reducing the production cost and reducing the raw material consumption, the high-conversion and high-selectivity direct synthesis of 1,3-butadiene from acetylene is realized.

[0023] In a preferred embodiment, the selective catalytic hydrogenation reaction in step S2 uses PdM / α-Al2O3 as a catalyst, and the M element is one or more of Zn, Co, Ni and Cu. The carrier selected for the PdM / α-Al2O3 catalyst is α-Al2O3. Compared with other carriers, α-Al2O3 also has the characteristics of low acidity, high thermal stability and good pore structure, which is more conducive to the hydrogenation conversion of vinylacetylene. On this basis, in the preferred PdM / α-Al2O3 catalyst, the mass loading of PdM is 0.1-0.5%. Setting the loading amount of the active substance in the catalyst within this range can comprehensively improve the conversion rate of vinylacetylene catalytic semi-hydrogenation and the selectivity of 1,3-butadiene. Moreover, since the single Pd-loaded catalyst has high activity and alkynes are easily over-hydrogenated to alkanes, and Co and Ni catalysts need to carry out catalytic reactions under high-pressure hydrogen conditions, with relatively high production safety requirements, therefore, in the preferred PdM / α-Al2O3 catalyst, the weight ratio of Pd to the M element is (1-5):5, so as to give full play to the catalytic role of Pd to a greater extent, improve the yield and selectivity of 1,3-butadiene, and at the same time cooperate to control the production cost. Moreover, through a large number of experiments and comparisons, the inventor found that when M in the catalyst simultaneously includes Cu and Ni, the obtained catalyst can greatly improve both the conversion rate of vinylacetylene catalytic semi-hydrogenation and the selectivity of 1,3-butadiene during application, and this effect may be attributed to the synergistic effect between Cu and Ni metal elements.

[0024] To obtain a PdM / α-Al2O3 catalyst with better catalytic performance, in a typical embodiment, regarding its synthesis, it includes the following steps: (1) Add Pd(OAc)2 and the nitrate of element M to an aqueous solution containing α-Al2O3, stir, impregnate and adsorb, and then remove the water to obtain a solid powder; (2) Subject the solid powder to a reduction reaction to obtain the PdM / α-Al2O3 catalyst. The selective catalytic hydrogenation reaction adopted in the present invention is prepared by a simple impregnation method and a calcination reduction method. The preparation method of the catalyst is simple, the conditions are mild, and the cost is low, and it has high selectivity for vinylacetylene catalytic hydrogenation.

[0025] Since in the preparation process of the above PdM / α-Al2O3 catalyst, the metal in the system may be oxidized and converted into the corresponding metal oxide, and its catalytic activity is also correspondingly reduced. Therefore, as described in step (2), it needs to be reduced. In a preferred embodiment, the temperature of the reduction reaction is 200-400 °C. Reduction at this temperature results in more suitable particle sizes and distributions of the active metals on the support, so that higher conversion rates of vinylacetylene and selectivities of 1,3-butadiene can be achieved during the catalytic process. To improve the stability of the selective catalytic hydrogenation reaction and better control the degree of the hydrogenation reaction, the preferred reduction atmosphere is a H2 / Ar flow, and the preferred volume ratio of H2 to Ar is 1:(2-4).

[0026] In a typical embodiment, to balance the intensity of the hydrogenation reaction and comprehensively consider the conversion rate of vinylacetylene and the selectivity of 1,3-butadiene, the volume ratio of the initial reaction gas to hydrogen in the selective catalytic hydrogenation reaction in step S2 is set to (80-100):(15-30) to optimize the experimental results of the final catalytic synthesis. Preferably, to further reduce costs, the selective catalytic hydrogenation reaction is carried out at room temperature, and the specific temperature range is 15-30 °C.

[0027] Since acetylene dimerization is a slow reaction, in order to reduce the transfer resistance of the acetylene dimerization reaction in step S1 and improve its conversion rate, acetylene is introduced into reactor I in the form of an acetylene / nitrogen mixture, and the volume content of acetylene in the acetylene / nitrogen mixture is 15-30%. Selecting the acetylene volume content within this range is beneficial to increasing the formation rate of its product vinylacetylene while ensuring the safety of this dimerization reaction.

[0028] Furthermore, the acetylene is continuously introduced into a reaction solution including water, cuprous chloride, ammonium chloride and hydrogen chloride to carry out the acetylene dimerization catalytic reaction. The acetylene dimerization catalytic reaction system used in the present invention is a Niewland system, and the specific composition is as described above. The raw materials in the system are low in price, the equipment involved is simple and easy to operate, and the application in the present invention can reduce the production cost to a greater extent and increase the added value of the final 1,3-butadiene product.

[0029] In a typical embodiment, hydrogen chloride is added in the form of hydrochloric acid solution, and the concentration of the hydrochloric acid solution is 2-5 mol / L. Based on the above content, in the Niewland system, the supramolecular structure formed by cuprous chloride and ammonium chloride is the catalytic active center, in which the active body that plays a catalytic role is CuCl2 - 、Cu2Cl3 - 、Cu3Cl4 - and Cu4Cl5 - The present invention relates to a method for preparing a catalyst for the reaction of a catalyst. The catalyst is preferably prepared by mixing a plurality of catalysts, wherein the catalyst is provided with ...

[0030] In a preferred embodiment, the reaction temperature in the reactor I is set to 80-100° C. On this basis, the reaction temperature in the reactor I is further preferably set to 90-95° C., so as to improve the acetylene conversion rate while reducing the occurrence of side reactions and the formation of polymers as much as possible, thereby increasing the yield of the intermediate product, namely vinyl acetylene.

[0031] In several typical embodiments, the yield of vinyl acetylene in step S1 is 70-77%; the conversion rate of the selective catalytic hydrogenation reaction in step S2 is 72-98%, and the selectivity of 1,3-butadiene is >62%, that is, a high conversion rate and a high selectivity of 1,3-butadiene are achieved.

[0032] The present application is further described in detail below in conjunction with specific embodiments. These embodiments should not be construed as limiting the scope of protection claimed in the present application.

[0033] Unless otherwise defined, all technical terms used hereinafter have the same meaning as commonly understood by those skilled in the art. The technical terms used herein are only for the purpose of describing specific embodiments and are not intended to limit the scope of protection of the present invention.

[0034] Example 1

[0035] A method for the continuous catalytic conversion of acetylene to synthesize 1,3-butadiene:

[0036] Preparation of the selective catalytic hydrogenation catalyst PdCu / α-Al2O3: Add 100 g of α-Al2O3 support material into a reactor containing 500 mL of distilled water, ultrasonically disperse evenly, then add 0.3 g of Pd(OAc)2 and 0.4 g of Cu(NO3)2 into the above mixed system, slowly stir and impregnate for adsorption at room temperature, and then remove the solvent by rotary evaporation; place the obtained solid powder in a sealed tubular furnace and reduce it at high temperature in a reducing atmosphere. The reducing atmosphere is H2 / Ar flow (V / V, 1:3), the reduction temperature is 400 °C, and the reducing gas flow rate is 20 mL / min; after reduction for 2 h, cool to room temperature to obtain the PdCu / α-Al2O3 catalyst; in the obtained PdCu / α-Al2O3 catalyst, the weight ratio of Pd to Cu is 2:5, and the loading amount of PdCu is 0.3 wt%.

[0037] Catalytic synthesis method: Add 80 mL of water, 40 g of cuprous chloride, 40 g of ammonium chloride, and 4 mL of 3 mol / L HCl into reactor I, stir and dissolve; then set the reaction temperature to 90 °C, and under vigorous stirring, bubble an acetylene / nitrogen mixture with an acetylene volume content of 30% and a flow rate of 100 mL / min into the reaction solution in reactor I to carry out the acetylene dimerization catalytic reaction; the primary reaction gas flowing out of reactor I directly enters reactor II filled with the above PdCu / α-Al2O3 catalyst at a flow rate of 80 mL / min, and at the same time, introduce H2 with a flow rate of 20 mL / min into reactor II, and catalytically hydrogenate vinylacetylene selectively at room temperature to synthesize 1,3-butadiene. The reaction route involved is shown in Figure 1 .

[0038] Example 2

[0039] A method for the continuous catalytic conversion of acetylene to synthesize 1,3-butadiene:

[0040] Add 60 mL of water, 30 g of cuprous chloride, 30 g of ammonium chloride, and 3 mL of 3 mol / L HCl into reactor I, and stir to dissolve. Set the reaction temperature at 80 °C, and under vigorous stirring, introduce an acetylene / nitrogen mixture with an acetylene volume content of 30% and a flow rate of 100 mL / min into the reaction solution in reactor I to carry out the acetylene dimerization catalytic reaction. The primary reaction gas flowing out of reactor I directly enters reactor II filled with the PdCu / α-Al2O3 catalyst obtained in Example 1 at a flow rate of 90 mL / min. At the same time, introduce H2 with a flow rate of 20 mL / min into reactor II, and catalytically hydrogenate vinylacetylene selectively to synthesize 1,3-butadiene at room temperature.

[0041] Example 3

[0042] A method for the continuous catalytic conversion of acetylene to synthesize 1,3-butadiene:

[0043] The difference between this example and Example 1 is that the catalyst for the selective catalytic hydrogenation reaction is PdZn / α-Al2O3. The specific experimental parameters involved in the synthesis are referred to those in Example 1. The weight ratio of Pd to Zn in PdZn / α-Al2O3 is also 2:5, and the loading amount of PdZn is also 0.3 wt%.

[0044] Example 4

[0045] A method for the continuous catalytic conversion of acetylene to synthesize 1,3-butadiene:

[0046] The difference between this example and Example 1 is that the catalyst for the selective catalytic hydrogenation reaction is PdCo / α-Al2O3. The specific experimental parameters involved in the synthesis are referred to those in Example 1. The weight ratio of Pd to Co in PdZn / α-Al2O3 is also 2:5, and the loading amount of PdCo is also 0.3 wt%.

[0047] Example 5

[0048] A method for the continuous catalytic conversion of acetylene to synthesize 1,3-butadiene:

[0049] The difference between this example and Example 1 is that the catalyst for the selective catalytic hydrogenation reaction is PdNi / α-Al2O3. The specific experimental parameters involved in the synthesis are referred to those in Example 1. The weight ratio of Pd to Ni in PdNi / α-Al2O3 is also 2:5, and the loading amount of PdNi is also 0.3 wt%.

[0050] Example 6

[0051] A method for the continuous catalytic conversion of acetylene to synthesize 1,3-butadiene:

[0052] The difference between this example and Example 1 is that the catalyst for the selective catalytic hydrogenation reaction is PdCuNi / α-Al2O3. The specific experimental parameters involved in the synthesis are referred to those in Example 1. The weight ratio of Pd to Cu and Ni in PdCuNi / α-Al2O3 is 1:5:5, and the loading amount of PdCuNi is also 0.3 wt%.

[0053] Example 7

[0054] A method for the continuous catalytic conversion of acetylene to synthesize 1,3-butadiene:

[0055] The difference between this example and Example 1 is that in the PdCu / α-Al2O3 catalyst, the weight ratio of Pd to Cu is 1:5, and the weight loading amount of PdCu is 0.1 wt%.

[0056] Example 8

[0057] A method for the continuous catalytic conversion of acetylene to synthesize 1,3-butadiene:

[0058] The difference between this example and Example 1 is that in the PdCu / α-Al2O3 catalyst, the weight ratio of Pd to Cu is 1:1, and the weight loading amount of PdCu is 0.5 wt%.

[0059] Example 9

[0060] A method for the continuous catalytic conversion of acetylene to synthesize 1,3-butadiene:

[0061] The difference between this example and Example 1 is that in the PdCu / α-Al2O3 catalyst, the weight ratio of Pd to Cu is 1:10, and the weight loading amount of PdCu is 0.05 wt%.

[0062] Example 10

[0063] A method for the continuous catalytic conversion of acetylene to synthesize 1,3-butadiene:

[0064] The difference between this example and Example 1 is that in the PdCu / α-Al2O3 catalyst, the weight ratio of Pd to Cu is 2:1, and the weight loading amount of PdCu is 1.0 wt%.

[0065] Example 11

[0066] A method for the continuous catalytic conversion of acetylene to synthesize 1,3-butadiene:

[0067] The difference between this example and Example 1 is that during the preparation of the PdCu / α-Al2O3 catalyst, the reduction temperature is 450 °C, the reduction atmosphere is H2 / Ar flow (V / V, 1:5), and the reduction gas flow rate is 35 mL / min.

[0068] Example 12

[0069] A method for continuously catalytically converting acetylene to synthesize 1,3 - butadiene:

[0070] The difference between this example and Example 1 is that in the selective catalytic hydrogenation reaction, the gas flow rate of the initial reaction gas is 80 mL / min, and the gas flow rate of hydrogen is 15 mL / min, that is, the gas flow rate ratio of the two is 80:15.

[0071] Example 13

[0072] A method for continuously catalytically converting acetylene to synthesize 1,3 - butadiene:

[0073] The difference between this example and Example 1 is that in the selective catalytic hydrogenation reaction, the gas flow rate of the initial reaction gas is 100 mL / min, and the gas flow rate of hydrogen is 30 mL / min, that is, the gas flow rate ratio of the two is 100:30.

[0074] Example 14

[0075] A method for continuously catalytically converting acetylene to synthesize 1,3 - butadiene:

[0076] The difference between this example and Example 1 is that in the selective catalytic hydrogenation reaction, the gas flow rate of the initial reaction gas is 60 mL / min, and the gas flow rate of hydrogen is 40 mL / min, that is, the gas flow rate ratio of the two is 60:40.

[0077] Example 15

[0078] A method for continuously catalytically converting acetylene to synthesize 1,3 - butadiene:

[0079] The difference between this example and Example 1 is that in the selective catalytic hydrogenation reaction, the gas flow rate of the initial reaction gas is 120 mL / min, and the gas flow rate of hydrogen is 10 mL / min, that is, the gas flow rate ratio of the two is 120:10.

[0080] Example 16

[0081] A method for continuously catalytically converting acetylene to synthesize 1,3 - butadiene:

[0082] The difference between this example and Example 1 is that in the acetylene dimerization reaction, the volume content of acetylene in the acetylene / nitrogen mixed gas is 10%.

[0083] Example 17

[0084] A method for continuously catalytically converting acetylene to synthesize 1,3 - butadiene:

[0085] The difference between this embodiment and Embodiment 1 is that in the acetylene dimerization reaction, the volume content of acetylene in the acetylene / nitrogen mixture gas is 35%.

[0086] Embodiment 18

[0087] A method for continuously catalytically converting acetylene to synthesize 1,3 - butadiene:

[0088] The difference between this embodiment and Embodiment 1 is that in the acetylene dimerization reaction, the temperature in Reactor I is 95°C.

[0089] Embodiment 19

[0090] A method for continuously catalytically converting acetylene to synthesize 1,3 - butadiene:

[0091] The difference between this embodiment and Embodiment 1 is that in the acetylene dimerization reaction, the temperature in Reactor I is 100°C.

[0092] The gas flowing out from Reactor I and Reactor II in the above - mentioned embodiments and comparative examples was detected by a gas chromatograph to obtain the yield of vinylacetylene in Reactor I, the hydrogenation conversion rate of vinylacetylene in Reactor II, and the selectivity of 1,3 - butadiene, as shown in Table 1 for details.

[0093] Table 1

[0094]

[0095] From the above description, it can be seen that the above - mentioned embodiments of the present invention achieve the synthesis of 1,3 - butadiene directly from acetylene with high conversion rate and high selectivity of 1,3 - butadiene.

[0096] It should be noted that the terms "first", "second", etc. in the description and claims of this application are used to distinguish similar objects and do not necessarily need to describe a specific order or sequence. It should be understood that such terms can be interchanged under appropriate circumstances so that the embodiments of this application described here can be implemented in an order other than those described here, for example.

[0097] The above - mentioned are only the preferred embodiments of the present invention and are not used to limit the present invention. For those skilled in the art, the present invention can have various modifications and changes. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included within the protection scope of the present invention.

Claims

1. A method for continuously catalytically converting acetylene to synthesize 1,3-butadiene, characterized in that, It includes the following steps: Step S1: Using acetylene as a raw material, continuously introducing it into Reactor I for acetylene dimerization catalytic reaction to obtain a primary reaction gas, and the primary reaction gas includes vinylacetylene; Step S2: Continuously introducing the primary reaction gas and hydrogen into Reactor II for selective catalytic hydrogenation reaction to obtain 1,3-butadiene.

2. The method for continuously catalytically converting acetylene to synthesize 1,3-butadiene according to claim 1, wherein In the selective catalytic hydrogenation reaction in Step S2, PdM / α-Al2O3 is used as a catalyst, where the M element is one or more of Zn, Co, Ni, and Cu; Preferably, in the PdM / α-Al2O3 catalyst, the mass loading of PdM is 0.1-0.5%; Preferably, in the PdM / α-Al2O3 catalyst, the mass ratio of Pd to the M element is (1-5):

5.

3. The method for continuously catalytically converting acetylene to synthesize 1,3-butadiene according to claim 2, wherein The PdM / α-Al2O3 catalyst is synthesized by the following steps: (1) Adding Pd(OAc)2 and the nitrate of the M element to an aqueous dispersion containing the α-Al2O3, stirring, impregnating, adsorbing, and then removing water to obtain a solid powder; (2) Subjecting the solid powder to a reduction reaction to obtain the PdM / α-Al2O3 catalyst.

4. The method for continuously catalytically converting acetylene to synthesize 1,3-butadiene according to claim 3, wherein In Step (2), the temperature of the reduction reaction is 200-400 °C, and the reduction atmosphere is a H2 / Ar stream, preferably the volume ratio of H2 to Ar is 1:(2-4).

5. The method for continuously catalytically converting acetylene to synthesize 1,3-butadiene according to any one of claims 1 to 4, characterized in that, In the selective catalytic hydrogenation reaction in Step S2, the volume ratio of the gas flow rates of the primary reaction gas and hydrogen is (80-100):(15-30); preferably, the selective catalytic hydrogenation reaction is carried out at room temperature.

6. The method for continuously catalytically converting acetylene to synthesize 1,3-butadiene according to any one of claims 1 to 5, characterized in that, In Step S1, the acetylene is introduced into Reactor I in the form of an acetylene / nitrogen mixture, and the volume content of acetylene in the acetylene / nitrogen mixture is 15-30%.

7. The method for continuously catalytically converting acetylene to synthesize 1,3-butadiene according to any one of claims 1 to 6, characterized in that, Continuously introducing the acetylene into a reaction solution including water, cuprous chloride, ammonium chloride, and hydrogen chloride for the acetylene dimerization catalytic reaction.

8. The method for continuously catalytically converting acetylene to synthesize 1,3-butadiene according to claim 7, characterized in that, The hydrogen chloride is added in the form of a hydrochloric acid solution, and the concentration of the hydrochloric acid solution is 2-5 mol / L; preferably, the weight ratio of cuprous chloride to ammonium chloride in the reaction solution is (20-40):(15-40); preferably, the volume ratio of the hydrochloric acid solution to the reaction solution for the acetylene dimerization catalytic reaction is (2-5):(50-100); preferably, the mass concentration of cuprous chloride in the reaction solution is 23-25%.

9. The method for continuously catalytically converting acetylene to synthesize 1,3-butadiene according to any one of claims 1 to 8, characterized in that, The reaction temperature in Reactor I is 80-100 °C, preferably 90-95 °C.

10. The method for continuously catalytically converting acetylene to synthesize 1,3-butadiene according to any one of claims 1 to 9, characterized in that, In Step S1, the yield of vinylacetylene is 70-77%; in Step S2, the conversion rate of the selective catalytic hydrogenation reaction is 72-98%, and the selectivity of 1,3-butadiene > 62%.

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