Catalyst, system and method for preparing succinic anhydride by carbonylation of ethylene oxide

Abstract

The invention relates to a catalyst, system and method for preparing butanedioic anhydride by carbonylation of ethylene oxide, and the method comprises the following steps: ethylene oxide, carbon monoxide, a solvent and a carbonylation catalyst are completely converted in a carbonylation reactor to generate butanedioic anhydride, and the catalyst is a compound of aluminum chloride phthalocyanine and cobalt carbonyl; the reacted material enters a high-pressure gas-liquid separator, carbon monoxide is extracted from the top and circularly returns to the reactor, a liquid-phase product with a catalyst is separated from the bottom and enters an evaporator, a solvent and succinic anhydride are extracted from the top and enter a solvent recovery tower, and a solid catalyst is obtained from the bottom and enters a catalyst preparation tank; a solvent extracted from the top of the solvent recovery tower enters a catalyst preparation tank, a catalyst solution is prepared again, and butanedioic anhydride is extracted from the bottom of the tower. Compared with the prior art, the method is good in atom economy, low in raw material cost, high in catalyst activity, good in stability, simple and efficient in process, high in production continuity degree, simple in subsequent separation and purification, high in product purity and suitable for large-scale production.

Description

Technical Field

[0001] The present invention relates to the technical field of carbonylation of epoxy compounds, and in particular to a catalyst, system and method for preparing succinic anhydride by carbonylation of ethylene oxide. Background Art

[0002] Succinic anhydride (SA) is an important chemical, commonly used as an intermediate and fine chemical raw material for organic synthesis. It is widely used in the fields of medicine, pesticides, food, petrochemicals, building materials, synthetic resins and dyes. In the petrochemical industry, succinic anhydride can be used to produce many downstream products, such as γ-butyrolactone, tetrahydrofuran, and 1,4-butanediol. Among them, 1,4-butanediol can be used as an organic raw material to synthesize a new green biodegradable plastic polybutylene succinate (PBS). PBS contains an easily hydrolyzed ester group in its structure and is easily decomposed by microorganisms in nature. Therefore, it has quickly become one of the hot research materials for general biodegradable plastics and has broad market prospects. With the promulgation and implementation of the "plastic ban" in various countries, the market demand for biodegradable plastics has increased year by year, bringing about a surge in demand for upstream raw materials. In addition, succinic anhydride has a very wide range of uses, resulting in a situation where succinic anhydride is in short supply worldwide. my country's succinic anhydride mainly relies on foreign imports, and domestic enterprises do not yet have a mature industrial production process for succinic anhydride. Therefore, it is urgent to develop a succinic anhydride synthesis method with industrial application prospects.

[0003] At present, the common methods for synthesizing succinic anhydride include maleic anhydride method, succinic acid dehydration method and carbonylation method. The maleic anhydride method includes electrolytic reduction method and catalytic hydrogenation method. The electrolytic reduction method has high energy consumption and high cost, so its application prospects are poor. The gas phase catalytic hydrogenation method is difficult to control the degree of hydrogenation, and there are many by-products, which makes it difficult to produce on a large scale. The advantages of the liquid phase catalytic hydrogenation method are high conversion rate, high yield and no obvious side reactions, but the disadvantage is that the process flow is mostly intermittent production, and the continuous production technology is not yet mature. The succinic acid dehydration method is limited by the small source of raw material succinic acid, which mainly comes from the catalytic hydrogenation of maleic anhydride, with high cost, and the generated succinic anhydride is easily hydrolyzed back to succinic acid, so the economic efficiency of this process route is low.

[0004] The ethylene oxide carbonylation process uses ethylene oxide and carbon monoxide as raw materials, and produces succinic anhydride through two carbonylation reactions. It is a green synthetic route with atom economy. The ethylene oxide carbonylation reaction was first proposed by Heck et al. (J. Am. Chem. Soc., 1963, 85(10): 1460-1463) in 1963. The catalyst is HCo(CO)4 / Co(CO)4 -. Subsequently, researchers have reported a variety of catalysts for the carbonylation of epoxides. However, most of the catalysts are mainly used for the selective synthesis of β-lactone by carbonylation of ethylene oxide, and there are few studies on succinic anhydride. Among them, the most representative is the research of Coates et al. from Cornell University in the United States (Angew. Chem. Int. Ed. Engl., 2002, 41 (15): 2781-2784; J. Am. Chem. Soc., 2002, 124 (7): 1174-1175; WO3050154, 2003). They systematically proposed a composite catalyst of Lewis acid and cobalt carbonyl for the first time, and proved that cobalt carbonyl is the core component of the catalytic system, and Lewis acid is the key to improving the activity of carbonylation of epoxides. Meanwhile, Coates et al. used tetrachlorophenylporphyrin aluminum chloride to catalyze the carbonylation of epoxy compounds to produce succinic anhydride at 90°C, and obtained a succinic anhydride yield of 98% (J.Am.Chem.Soc., 2007, 129(7):4948-4960). However, the reported porphyrin ligand catalyst is complicated to prepare, has high cost, and has harsh operating conditions, and is not suitable for the industrial production of succinic anhydride. In addition, there are multiple patents at home and abroad that report on epoxy compound carbonylation catalysts.

[0005] CN201180047249.2 discloses a method for synthesizing succinic anhydride, and the catalyst used is meta-tetrakis (4-chlorophenyl) porphyrin / cobalt carbonyl and a metal carbonyl compound; CN202211600026.0 discloses a metal nitrogen flip porphyrin-cobalt carbonyl multifunctional catalyst, which accelerates the ring-opening process of ethylene oxide; CN201580020704.8 discloses a catalyst of a combination of a Lewis acid metal compound of a tethered metal coordination group and a metal carbonyl, wherein the Lewis acid is mainly a porphyrin ligand and a salene ligand. It can be seen that porphyrin metal compounds are the most reported Lewis acid ligands for preparing succinic anhydride by carbonylation of ethylene oxide, but the preparation of the raw materials is complicated, the cost is high, and it is unstable, and when reacting with cobalt carbonyl to synthesize the complex catalyst, the preparation method is also relatively complicated. In order to realize the large-scale production of succinic anhydride prepared by carbonylation of ethylene oxide, it is not only necessary to further design and optimize the catalyst, but more importantly, to establish a complete carbonylation reaction separation process. For the ethylene oxide carbonylation process, US9156803B2 discloses a method for preparing succinic anhydride from ethylene oxide, using a first catalyst to promote a first carbonylation reaction, and using a second catalyst different from the first catalyst to promote a second carbonylation reaction. The catalyst system is complex, and crystallization separation is performed after the reaction to separate the generated anhydride from the catalyst and the solvent. However, in industry, the crystallization process is complex, and the catalyst is easily wrapped in the succinic anhydride crystals, which affects the purity of the anhydride and is difficult to produce on a large scale. Summary of the invention

[0006] The purpose of the present invention is to overcome the defects of the above-mentioned prior art and provide a catalyst, system and method for preparing succinic anhydride by carbonylation of ethylene oxide. The present invention uses ethylene oxide and carbon monoxide as raw materials, has good atom economy, low raw material cost, high catalyst activity and good stability, simple and efficient process, high degree of production continuity, simple subsequent separation and purification, high product purity, and is suitable for large-scale production.

[0007] The purpose of the present invention can be achieved by the following technical solutions:

[0008] The first object of the present invention is to provide a method for preparing succinic anhydride by carbonylation of ethylene oxide, the method comprising the following steps: ethylene oxide, carbon monoxide, solvent and carbonylation catalyst enter a carbonylation reactor, ethylene oxide is completely converted in the carbonylation reactor to generate succinic anhydride, and a reacted material is obtained, wherein the catalyst is a complex of aluminum phthalocyanine chloride and cobalt carbonyl; the reacted material enters a high-pressure gas-liquid separator, carbon monoxide is extracted from the top of the high-pressure gas-liquid separator and recycled back to the reactor, a liquid phase product with the catalyst is separated from the bottom of the high-pressure gas-liquid separator and enters an evaporator, the solvent and succinic anhydride extracted from the top of the evaporator enter a solvent recovery tower, a solid catalyst is obtained from the bottom of the evaporator, the solid catalyst enters a catalyst configuration tank, a catalyst solution is reconfigured, and the configured catalyst solution enters the reactor through a catalyst pump; the solvent is extracted from the top of the solvent recovery tower and enters the catalyst configuration tank, the catalyst solution is reconfigured, and the succinic anhydride product is extracted from the bottom of the solvent recovery tower.

[0009] In the carbonylation reaction of ethylene oxide, ethylene oxide and carbon monoxide (CO) react, and first carbonylation occurs to generate a β-propiolactone intermediate, and then β-propiolactone is further carbonylated to generate succinic anhydride, and the two are a series reaction. Therefore, in the carbonylation process of ethylene oxide, the reaction temperature, time and the molar ratio of ethylene oxide and carbon monoxide in the raw materials play an important role in the conversion rate of EO and the selectivity of succinic anhydride. Under the catalyst and reaction conditions, when the molar ratio of CO to EO is not less than 2:1, by regulating the reaction temperature and time, the complete conversion of EO and the high selectivity of succinic anhydride can be achieved.

[0010] Furthermore, in the carbonylation catalyst (catalytic complex), the molar ratio of aluminum phthalocyanine chloride and Co2(CO)8 is 10:1-1:10. The appropriate ratio of aluminum phthalocyanine chloride and cobalt carbonyl (Co2(CO)8) can synergistically catalyze the secondary carbonylation reaction of EO, and has high activity and selectivity for the carbonylation of ethylene oxide (EO) to prepare succinic anhydride.

[0011] Furthermore, the solvent is one or a mixture of several of tetrahydrofuran (THF), diethylene glycol dimethyl ether, β-propiolactone, 1,4-dioxane, 1,3-dioxolane and toluene.

[0012] Furthermore, the molar ratio of the cobalt carbonyl in the carbonylation catalyst to the ethylene oxide is 1:50 to 1:500, and the concentration of ethylene oxide in the solvent is 1.0-5.0M.

[0013] Furthermore, the molar ratio of carbon monoxide to ethylene oxide is 2:1-5:1.

[0014] Furthermore, the reaction pressure during the complete conversion of ethylene oxide in the carbonylation reactor is 3.0-6.0 MPa, and the reaction temperature is 60°C-100°C.

[0015] Furthermore, the operating pressure of the high-pressure gas-liquid separator is 3.0-6.0MPa, and the operating temperature of the high-pressure gas-liquid separator is -30-30°C; the operating pressure of the evaporator is 2-15kPa, and the operating temperature of the evaporator is 150-200°C; the operating pressure of the solvent recovery tower is reduced pressure or normal pressure, and the operating temperature is 120-200°C.

[0016] Furthermore, the reconfiguration of the catalyst solution refers to: obtaining a solid catalyst at the bottom of the evaporator and extracting a solvent from the top of the solvent recovery tower, and additionally adding a solvent and a carbonylation catalyst to adjust the ratio to reconfigure the catalyst solution.

[0017] The second object of the present invention is to provide a catalyst for preparing succinic anhydride by carbonylation of ethylene oxide. The catalyst is used to realize the method for preparing succinic anhydride by carbonylation of ethylene oxide. The catalyst is a carbonylation catalyst; the carbonylation catalyst is a complex of phthalocyanine aluminum chloride and carbonyl cobalt.

[0018] Furthermore, the molar ratio of the phthalocyanine aluminum chloride to cobalt carbonyl (Co2(CO)8) is 10:1-1:10.

[0019] The second object of the present invention is to provide a system for preparing succinic anhydride by carbonylation of ethylene oxide, wherein the system is used to implement a method for preparing succinic anhydride by carbonylation of ethylene oxide, and the system comprises a catalyst pump, a carbonylation reactor, a high-pressure gas-liquid separator, an evaporator, a catalyst configuration tank, and a solvent recovery tower; the carbonylation reactor is connected to the high-pressure gas-liquid separator; the high-pressure gas-liquid separator is connected to the evaporator; the evaporator is connected to the solvent recovery tower; the evaporator is connected to the catalyst configuration tank; the solvent recovery tower is connected to the catalyst configuration tank; the catalyst configuration tank is connected to the carbonylation reactor via a catalyst pump.

[0020] Furthermore, the carbonylation reactor is connected to the high-pressure gas-liquid separator through a pipeline; the high-pressure gas-liquid separator is connected to the evaporator through a pipeline; the evaporator is connected to the solvent recovery tower through a pipeline; the evaporator is connected to the catalyst configuration tank through a pipeline; the solvent recovery tower is connected to the catalyst configuration tank through a pipeline; the catalyst configuration tank is connected to the carbonylation reactor through a pipeline and a catalyst pump.

[0021] The present invention relates to a catalyst, system and method for preparing succinic anhydride by carbonylation of ethylene oxide, which specifically comprises the following steps: ethylene oxide is completely converted in a carbonylation reactor in the presence of carbon monoxide, a solvent and a carbonylation catalyst to generate succinic anhydride, wherein the catalyst is a composite of phthalocyanine aluminum chloride and carbonyl cobalt; the reacted material enters a high-pressure gas-liquid separator, carbon monoxide is extracted from the top of the high-pressure gas-liquid separator and circulated back to the reactor, a liquid phase product with a catalyst is separated from the bottom of the high-pressure gas-liquid separator and enters an evaporator, solvent and succinic anhydride are extracted from the top of the evaporator and enter a solvent recovery tower, a solid catalyst is obtained from the bottom of the evaporator and enters a catalyst configuration tank; solvent is extracted from the top of the solvent recovery tower and enters the catalyst configuration tank, and a catalyst solution is reconfigured, and succinic anhydride is extracted from the bottom of the solvent recovery tower and enters a refining tower. Compared with the prior art, the present invention uses ethylene oxide and carbon monoxide as raw materials, has good atomic economy, low raw material cost, high catalyst activity, good stability, simple and efficient process, high degree of production continuity, simple subsequent separation and purification, high product purity, and is suitable for large-scale production.

[0022] Compared with the prior art, the present invention has the following beneficial effects:

[0023] 1) The present invention provides a catalyst, system and method for preparing succinic anhydride by carbonylation of ethylene oxide, which has a simple preparation process, high activity, good stability and can be recycled. The carbonylation catalyst is a complex of phthalocyanine aluminum chloride and Co2(CO)8, has high reaction activity, greatly reduces the residence time of raw materials, improves reaction efficiency, and ensures complete conversion of ethylene oxide.

[0024] 2) The present invention provides a catalyst, system and method for preparing succinic anhydride by carbonylation of ethylene oxide. The method for preparing succinic anhydride by carbonylation of ethylene oxide uses cheap carbon monoxide as a raw material, and the reaction has good atom economy.

[0025] 3) The present invention provides a catalyst, system and method for preparing succinic anhydride by carbonylation of ethylene oxide, which is a complete process flow for preparing succinic anhydride by carbonylation of ethylene oxide. Ethylene oxide and CO raw materials are subjected to carbonylation reaction and product separation to directly obtain high-purity succinic anhydride. The process is simple and efficient, the reaction efficiency is high, the production is highly continuous, the subsequent separation and purification is simple, the product purity is high, it is safe and reliable, the production cost is low, and it is suitable for large-scale production. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] Figure 1 Schematic diagram of the system for preparing succinic anhydride by carbonylation of ethylene oxide in an embodiment of the present invention.

[0027] in:

[0028] P101-catalyst pump; R101-carbonylation reactor; V101-high-pressure gas-liquid separator; V102-evaporator; V103-catalyst preparation tank; T101-solvent recovery tower. DETAILED DESCRIPTION

[0029] The present invention is described in detail below in conjunction with specific embodiments, which are only used to illustrate the present invention and are not used to limit the scope of protection of the present invention. The features such as component models, material names, connection structures, control methods, etc. that are not clearly described in this technical solution are regarded as common technical features disclosed in the prior art.

[0030] like Figure 1 As shown, the present invention provides a system for realizing a method for preparing succinic anhydride by carbonylation of ethylene oxide, the system comprising a catalyst pump P101, a carbonylation reactor R101, a high-pressure gas-liquid separator V101, an evaporator V102, a catalyst configuration tank V103, and a solvent recovery tower T101; the carbonylation reactor R101 is connected to the high-pressure gas-liquid separator V101 through a pipeline; the high-pressure gas-liquid separator V101 is connected to the evaporator V102 through a pipeline; the evaporator V102 is connected to the solvent recovery tower T101 through a pipeline; the evaporator V102 is connected to the catalyst configuration tank V103 through a pipeline; the solvent recovery tower T101 is connected to the catalyst configuration tank V103 through a pipeline; the catalyst configuration tank V103 is connected to the carbonylation reactor R101 through a pipeline and the catalyst pump P101.

[0031] Example 1

[0032] refer to Figure 1The present invention provides a catalyst and method for preparing succinic anhydride by carbonylation of ethylene oxide. Ethylene oxide, carbon monoxide, solvent and carbonylation catalyst enter carbonylation reactor R101. Ethylene oxide is completely converted in carbonylation reactor R101 to generate succinic anhydride. The catalyst is a composite of aluminum phthalocyanine chloride and cobalt carbonyl. The materials after the reaction enter high-pressure gas-liquid separator V101. Carbon monoxide is extracted from the top of high-pressure gas-liquid separator V101 and recycled back to reactor R101. Carbon monoxide is separated from the bottom of high-pressure gas-liquid separator V101. The liquid product with catalyst enters the evaporator V102, the solvent and succinic anhydride extracted from the top of the evaporator V102 enter the solvent recovery tower T101, the solid catalyst is obtained at the bottom of the evaporator V102, enters the catalyst preparation tank V103, the catalyst solution is reconfigured, and the configured catalyst enters the reactor R101 through the catalyst pump P101; the solvent extracted from the top of the solvent recovery tower T101 enters the catalyst preparation tank V103, the catalyst solution is reconfigured, and the succinic anhydride product is extracted from the bottom of the solvent recovery tower T101.

[0033] In one embodiment of the present invention, the carbonylation catalyst is a complex of aluminum phthalocyanine chloride and Co2(CO)8, and the molar ratio of aluminum phthalocyanine chloride to Co2(CO)8 is 1:1.

[0034] In one embodiment of the present invention, the carbonylation reaction solvent is THF.

[0035] In one embodiment of the present invention, the molar ratio of cobalt carbonyl to ethylene oxide in the carbonylation catalyst is 1:100, and the concentration of ethylene oxide in the solvent is 2.0M.

[0036] In one embodiment of the present invention, the molar ratio of carbon monoxide to ethylene oxide is 2:1.

[0037] In one embodiment of the present invention, the temperature of the carbonylation reactor R101 is 90° C., the pressure is 5.5 MPa, and the reaction residence time is 2 hours.

[0038] In one embodiment of the present invention, the operating pressure of the high-pressure gas-liquid separator V101 is 5.5 MPa, and the operating temperature of the high-pressure gas-liquid separator V101 is 30°C; the operating pressure of the evaporator V102 is 10 kPa, and the operating temperature of the evaporator V102 is 200°C; the operating pressure of the solvent recovery tower T101 is normal pressure and the temperature is 150°C.

[0039] Example 2

[0040] refer to Figure 1The present invention provides a catalyst and method for preparing succinic anhydride by carbonylation of ethylene oxide. Ethylene oxide, carbon monoxide, solvent and carbonylation catalyst enter carbonylation reactor R101. Ethylene oxide is completely converted in carbonylation reactor R101 to generate succinic anhydride. The catalyst is a composite of aluminum phthalocyanine chloride and cobalt carbonyl. The materials after the reaction enter high-pressure gas-liquid separator V101. Carbon monoxide is extracted from the top of high-pressure gas-liquid separator V101 and recycled back to reactor R101. Carbon monoxide is separated from the bottom of high-pressure gas-liquid separator V101. The liquid product with catalyst enters the evaporator V102, the solvent and succinic anhydride extracted from the top of the evaporator V102 enter the solvent recovery tower T101, the solid catalyst is obtained at the bottom of the evaporator V102, enters the catalyst preparation tank V103, the catalyst solution is reconfigured, and the configured catalyst enters the reactor R101 through the catalyst pump P101; the solvent extracted from the top of the solvent recovery tower T101 enters the catalyst preparation tank V103, the catalyst solution is reconfigured, and the succinic anhydride product is extracted from the bottom of the solvent recovery tower T101.

[0041] In one embodiment of the present invention, the carbonylation catalyst is a complex of aluminum phthalocyanine chloride and Co2(CO)8, and the molar ratio of aluminum phthalocyanine chloride to Co2(CO)8 is 1:1.

[0042] In one embodiment of the present invention, the carbonylation reaction solvent is THF.

[0043] In one embodiment of the present invention, the molar ratio of cobalt carbonyl to ethylene oxide in the carbonylation catalyst is 0.5:100, and the concentration of ethylene oxide in the solvent is 2.0M.

[0044] In one embodiment of the present invention, the temperature of the carbonylation reactor R101 is 100° C., the pressure is 5.5 MPa, and the reaction residence time is 1 hour.

[0045] In one embodiment of the present invention, the operating pressure of the high-pressure gas-liquid separator V101 is 5.5 MPa, and the operating temperature of the high-pressure gas-liquid separator V101 is 30°C; the operating pressure of the evaporator V102 is 10 kPa, and the operating temperature of the evaporator V102 is 200°C; the operating pressure of the solvent recovery tower T101 is normal pressure and the temperature is 150°C.

[0046] The products in Examples 1 and 2 are analyzed below. The results are shown in Table 1.

[0047] Table 1. Results of carbonylation reaction of ethylene oxide and carbon monoxide

[0048] Example EO conversion, % Succinic anhydride yield, % 1 100 100 2 100 100

[0049] It can be seen from Table 1 that in Examples 1 and 2, the conversion rate of ethylene oxide can reach 100%, and the yield of succinic anhydride can reach 100%.

[0050] The above description of the embodiments is to facilitate the understanding and use of the invention by those skilled in the art. It is obvious that those skilled in the art can easily make various modifications to these embodiments and apply the general principles described herein to other embodiments without creative work. Therefore, the present invention is not limited to the above embodiments, and improvements and modifications made by those skilled in the art based on the disclosure of the present invention without departing from the scope of the present invention should be within the scope of protection of the present invention.

Claims

1. A method for preparing succinic anhydride by carbonylation of ethylene oxide, characterized in that: The method comprises the following steps: Ethylene oxide, carbon monoxide, solvent and carbonylation catalyst enter into carbonylation reactor (R101), ethylene oxide is completely converted in carbonylation reactor (R101) to generate succinic anhydride, and a reacted material is obtained, wherein the carbonylation catalyst is a composite of aluminum phthalocyanine chloride and cobalt carbonyl; The reacted materials enter the high-pressure gas-liquid separator (V101), carbon monoxide is extracted from the top of the high-pressure gas-liquid separator (V101) and recycled back to the reactor (R101), and the liquid phase product with catalyst is separated from the bottom of the high-pressure gas-liquid separator (V101) and enters the evaporator (V102); The solvent and succinic anhydride extracted from the top of the evaporator (V102) enter the solvent recovery tower (T101), and the solid catalyst is obtained at the bottom of the evaporator (V102). The solid catalyst enters the catalyst configuration tank (V103), and the catalyst solution is reconfigured. The configured catalyst solution enters the (R101) reactor through the catalyst pump (P101); The solvent is taken out from the top of the solvent recovery tower (T101) and enters the catalyst preparation tank (V103) to re-prepare the catalyst solution, and the succinic anhydride product is taken out from the bottom of the solvent recovery tower (T101).

2. The method for preparing succinic anhydride by carbonylation of ethylene oxide according to claim 1, characterized in that: The reconfiguration of the catalyst solution refers to: obtaining a solid catalyst at the bottom of the evaporator (V102) and extracting a solvent from the top of the solvent recovery tower (T101), and additionally adding a solvent and a carbonylation catalyst to adjust the ratio to reconfigure the catalyst solution.

3. The method for preparing succinic anhydride by carbonylation of ethylene oxide according to claim 1, characterized in that: The molar ratio of phthalocyanine aluminum chloride to cobalt carbonyl in the carbonylation catalyst is 10:1-1:

10.

4. The method for preparing succinic anhydride by carbonylation of ethylene oxide according to claim 1, characterized in that: The solvent is one or a mixture of tetrahydrofuran, diethylene glycol dimethyl ether, β-propiolactone, 1,4-dioxane, 1,3-dioxolane and toluene.

5. The method for preparing succinic anhydride by carbonylation of ethylene oxide according to claim 1, characterized in that: The molar ratio of carbonyl cobalt to ethylene oxide in the carbonylation catalyst is 1:50-1:500, and the concentration of ethylene oxide in the solvent is 1.0-5.0M.

6. The method for preparing succinic anhydride by carbonylation of ethylene oxide according to claim 1, characterized in that: The reaction pressure during the complete conversion of ethylene oxide in the carbonylation reactor is 3.0-6.0 MPa and the reaction temperature is 60°C-100°C.

7. The method for preparing succinic anhydride by carbonylation of ethylene oxide according to claim 1, characterized in that: The operating pressure of the high-pressure gas-liquid separator (V101) is 3.0-6.0 MPa, and the operating temperature of the high-pressure gas-liquid separator (V101) is -30-30°C; The operating pressure of the evaporator (V102) is 2-15 kPa, and the operating temperature of the evaporator (V102) is 150-200°C; The operating pressure of the solvent recovery tower (T101) is reduced pressure or normal pressure, and the operating temperature is 120-200°C.

8. The method for preparing succinic anhydride by carbonylation of ethylene oxide according to claim 1, characterized in that: The molar ratio of carbon monoxide to ethylene oxide is 2:1-5:

1.

9. A catalyst for realizing the method for preparing succinic anhydride by carbonylation of ethylene oxide as claimed in any one of claims 1 to 8, characterized in that: The catalyst is a carbonylation catalyst; The carbonylation catalyst is a complex of phthalocyanine aluminum chloride and carbonyl cobalt.

10. A system for implementing the method for preparing succinic anhydride by carbonylation of ethylene oxide as claimed in any one of claims 1 to 8, characterized in that: The system comprises a catalyst pump (P101), a carbonylation reactor (R101), a high-pressure gas-liquid separator (V101), an evaporator (V102), a catalyst configuration tank (V103), and a solvent recovery tower (T101); The carbonylation reactor (R101) is connected to a high-pressure gas-liquid separator (V101); The high-pressure gas-liquid separator (V101) is connected to the evaporator (V102); The evaporator (V102) is connected to the solvent recovery tower (T101); The evaporator (V102) is connected to the catalyst configuration tank (V103); The solvent recovery tower (T101) is connected to the catalyst configuration tank (V103); The catalyst configuration tank (V103) is connected to the carbonylation reactor (R101) via a catalyst pump (P101).

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