Recycling and regenerating system and method of catalyst

Abstract

The invention discloses a catalyst recycling and regenerating system and method. The catalyst recycling and regenerating system comprises an advanced oxidation device and a first-stage recycling subsystem, the first-stage recovery subsystem comprises a first extraction agent storage tank, a first reaction kettle, a first centrifugal separator, a first vacuum separator and a first plate-and-frame filter press; the second-stage recovery subsystem comprises a second extraction agent storage tank, a second reaction kettle, a second centrifugal separator, a second vacuum separator and a second plate-and-frame filter press; and the third-stage recovery subsystem comprises a third extraction agent storage tank, a third reaction kettle, a third centrifugal separator, a third vacuum separator and a third plate-and-frame filter press. The recycling and regenerating method comprises the steps of S1 to S9. According to the method, the problem of environmental pollution caused by using strong acid and strong alkali is avoided, meanwhile, compared with heat treatment, mechanical grinding and other methods, the activity of the catalyst can be more effectively recovered, operation is relatively simple, cost is low, and remarkable economic value and environmental benefits are achieved.

Description

Technical Field

[0001] The present invention relates to the technical field of resource recovery and catalyst preparation, and in particular to a catalyst recovery and regeneration system and method. Background Art

[0002] Cu-Bi catalysts, due to their unique catalytic properties, have been widely used in a variety of organic synthesis reactions. For example, in the production of 1,4-butanediol (BDO) via the acetylene-aldehyde process, Cu-Bi catalysts can efficiently catalyze the acetylene-aldehyde reaction of formaldehyde and acetylene to produce 1,4-butynediol, which is further processed into 1,4-butanediol, an important chemical raw material. However, over long-term use, Cu-Bi catalysts gradually lose their activity, resulting in reduced reaction efficiency and the need for regular replacement. Currently, there are several main methods for treating spent Cu-Bi catalysts: 1. Direct disposal: This method is the simplest, but it will cause a huge waste of resources, and the discarded catalyst contains heavy metals such as Cu and Bi, which will cause serious pollution to the environment.

[0003] 2. Chemical leaching: Use a strong acid or alkaline solution to leach the spent catalyst, dissolving active components such as Cu and Bi in the solution. The catalyst is then recovered through precipitation, electrolysis, and other methods. This method has the advantage of relatively high recovery efficiency, but the disadvantages are that the chemical reagents used can pollute the environment, and the treatment process is complex and costly.

[0004] 3. Thermal regeneration: The spent catalyst is calcined or reduced at high temperatures to remove surface carbon deposits and other impurities, restoring some of the catalyst's activity. However, this method often only partially restores the catalyst's activity, and high-temperature treatment may also cause structural changes in the catalyst, affecting its ultimate catalytic performance.

[0005] 4. Mechanical Grinding Regeneration: Mechanical grinding is used to refine spent catalyst particles, increase specific surface area, and thus enhance activity. However, this method has limited recovery of catalyst activity, and the grinding process may introduce impurities that affect the catalyst's catalytic performance. Therefore, it is necessary to develop an efficient, environmentally friendly, and economical recycling system for spent Cu-Bi catalysts. Summary of the Invention

[0006] In view of the above-mentioned deficiencies in the prior art, the present invention provides a catalyst recovery and regeneration system and method.

[0007] In order to achieve the above-mentioned object of the invention, the technical solution adopted by the present invention is: A catalyst recovery and regeneration system is provided, comprising an advanced oxidation device and a first-stage recovery subsystem; the first-stage recovery subsystem comprises a first extractant storage tank, a first reactor, a first centrifugal separator, a first vacuum separator, and a first plate-frame filter press; a feed end of the first reactor is connected to an output end of the advanced oxidation device via a pipeline, a liquid inlet end of the first reactor is connected to an output end of the first extractant storage tank via a pipeline, a discharge end of the first reactor is connected to a feed end of the first centrifugal separator via a pipeline, a discharge end of the first centrifugal separator is connected to a discharge end of the first vacuum separator via a pipeline, a discharge end of the first vacuum separator is connected to a feed end of the first plate-frame filter press via a pipeline, and liquid outlet pipes of the first centrifugal separator, the first vacuum separator, and the first plate-frame filter press are all connected to the first extractant storage tank via a pipeline.

[0008] Furthermore, it also includes a second-stage recovery subsystem, which includes a second extractant storage tank, a second reactor, a second centrifugal separator, a second vacuum separator, and a second plate and frame filter press; the feed end of the second reactor is connected to the discharge end of the first plate and frame filter press through a first conveying pipeline, the liquid inlet end of the second reactor is connected to the output end of the second extractant storage tank through a pipeline, the discharge end of the second reactor is connected to the feed end of the second centrifugal separator through a pipeline, the discharge end of the second centrifugal separator is connected to the discharge end of the second vacuum separator through a pipeline, the discharge end of the second vacuum separator is connected to the feed end of the second plate and frame filter press through a pipeline, and the liquid outlet pipes of the second centrifugal separator, the second vacuum separator, and the second plate and frame filter press are all connected to the second extractant storage tank through a pipeline.

[0009] Furthermore, it also includes a third-level recovery subsystem, which includes a third extractant storage tank, a third reactor, a third centrifuge, a third vacuum separator and a third plate and frame filter press; the feed end of the third reactor is connected to the discharge end of the second plate and frame filter press through a pipeline, the liquid inlet end of the third reactor is connected to the output end of the third extractant storage tank through a second conveying pipeline, the discharge end of the third reactor is connected to the feed end of the third centrifuge through a pipeline, the discharge end of the third centrifuge is connected to the discharge end of the third vacuum separator through a pipeline, the discharge end of the third vacuum separator is connected to the feed end of the third plate and frame filter press through a pipeline, and the liquid outlet pipes of the third centrifuge, the third vacuum separator and the third plate and frame filter press are all connected to the third extractant storage tank through a pipeline.

[0010] Furthermore, the first conveying pipeline and the second conveying pipeline are both screw conveyors.

[0011] The catalyst recovery and regeneration method comprises the following steps: S1: Weigh a certain amount of spent Cu-Bi catalyst and dissolve it in the reaction water tank of the superoxide oxidation device; S2: Control the reaction temperature of the superoxide oxidation device during oxidation, oxidize the spent Cu-Bi catalyst for a period of time, and then transport it to the first reactor; S3: Add 300 mL of petroleum ether to the first reactor and stir evenly to allow the catalyst to fully contact the solvent. Heat the first reactor to 25°C, maintain normal pressure, and stir to react for 1 hour. S4: The mixture generated in the first reactor is subjected to solid-liquid separation by a first centrifugal separator, a first vacuum separator 10 and a first plate-frame filter press 11 to obtain a first organic phase and a first solid phase; S5: After filtering the first solid phase in step S4, transfer it to the second reactor, add 300 mL of toluene to the second reactor, stir evenly to allow the catalyst to fully contact with the solvent, raise the temperature in the second reactor to 55°C and the pressure to 0.25 MPa, and continue stirring and reacting for 2 hours; S6: After the reaction is completed, the mixture produced in the second reactor is passed through a second centrifugal separator, a second vacuum separator, and a second plate-frame filter press for solid-liquid separation to obtain a second organic phase and a second solid phase; S7: After filtering the second solid phase, transfer it to the third reactor, add 300 mL of methanol to the third reactor, stir evenly to allow the catalyst to fully contact with the solvent, set the temperature of the third reactor to 30°C and the pressure to normal pressure, and continue stirring and reacting for 2 hours; S8: After the reaction is completed, the mixture produced in the third reactor is passed through a third centrifugal separator, a third vacuum separator, and a third plate-frame filter press for solid-liquid separation to obtain a third organic matter and a third solid phase, and the third solid phase is filtered to obtain a regenerated spent Cu-Bi catalyst; S9: The regenerated waste Cu-Bi catalyst is mixed with the new catalyst in a mass ratio of 1:9 and used for the reaction of producing 1,4-butanediol by the acetylene aldehyde process.

[0012] Furthermore, in step S1, the concentration of the spent Cu-Bi catalyst in the reaction water tank of the superoxide oxidation device is less than 200 g / L.

[0013] Furthermore, the oxidation temperature in step S2 is 40° C. to 80° C., and the oxidation reaction time is 2 h to 4 h.

[0014] Furthermore, the temperature of the first reactor, the second reactor and the third reactor is 20° C. to 80° C., the pressure is normal pressure, the extraction time is 1 h to 3 h, and the stirring speed is 100 rpm to 1000 rpm.

[0015] Furthermore, the centrifugal speed of the first centrifugal separator, the second centrifugal separator and the third centrifugal separator is 1000rpm to 6000rpm, the vacuum degree of the first vacuum separator, the second vacuum separator and the third vacuum separator is 0.05Mpa to 0.1Mpa, and the extrusion separation pressure of the first plate and frame filter press, the second plate and frame filter press and the third plate and frame filter press is 1MPa to 7MPa.

[0016] The beneficial effects of the present invention are: The present invention.

[0017] The recycling and regeneration system of the present invention oxidizes the spent Cu-Bi catalyst, breaking the bonds of some mixed polymer carbon deposits (part of the carbon deposits are oxidized and removed in the form of gas), then uses an organic solvent for step-by-step extraction to gradually release the remaining carbon deposits into the organic solvent. Finally, after separation treatment, a solid phase rich in active components is obtained, which is mixed with a new catalyst and can be used to re-prepare the catalyst for the process.

[0018] The recovery and regeneration method of the present invention includes the steps of catalyst dispersion, advanced oxidation, cascade extraction, centrifugal separation, solid-liquid separation, and mixing with a new carrier to prepare the catalyst. Compared with existing technologies, the present invention avoids the use of strong acids and bases, reducing environmental pollution. It is also simple to operate, low-cost, and can effectively restore catalyst activity, achieving resource recycling, with significant economic and environmental benefits.

[0019] The advanced oxidation method of the present invention can break the bonds of the polymer carbon deposit components to facilitate subsequent cascade extraction. At the same time, part of the carbon deposit is oxidized into gas and removed, reducing the amount of subsequent extractant used. The cascade extraction uses organic solvents with different polarities, which can extract and separate the polar and non-polar carbon deposit components as completely as possible, thereby separating and obtaining high-purity Cu-Bi active components.

[0020] The method of the present invention avoids the environmental pollution problems caused by the use of strong acids and strong bases. Compared with methods such as heat treatment and mechanical grinding, it can more effectively restore the activity of the catalyst. In addition, the operation is relatively simple and the cost is low, and it has significant economic value and environmental benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0021] Figure 1 Schematic diagram of the structure of the catalyst recovery and regeneration system of the present invention; The main components in the figure are described as follows: 1. Material silo; 2. First extractant storage tank; 3. Second extractant storage tank; 4. Third extractant storage tank; 5. Advanced oxidation unit; 6. First reactor; 7. Second reactor; 8. Third reactor; 9. First centrifuge; 10. First vacuum separator; 11. First plate and frame filter press; 12. Second centrifuge; 13. Second vacuum separator; 14. Second plate and frame filter press; 15. Third centrifuge; 16. Third vacuum separator; 17. Third plate and frame filter press. DETAILED DESCRIPTION

[0022] The specific embodiments of the present invention are described below to facilitate understanding of the present invention by those skilled in the art. However, it should be clear that the present invention is not limited to the scope of the specific embodiments. For those skilled in the art, as long as various changes are within the spirit and scope of the present invention as defined and determined by the appended claims, these changes are obvious, and all inventions and creations utilizing the concepts of the present invention are protected.

[0023] Example 1 like Figure 1 As shown, the catalyst recovery and regeneration system includes a waste catalyst raw material storage bin 1, an advanced oxidation device 5, and a first-stage recovery subsystem. The advanced oxidation device 5 is a low-temperature plasma oxidation device or a superoxide oxidation device. The first-stage recovery subsystem includes a first extractant storage tank 2, a first reactor 6, a first centrifuge 9, a first vacuum separator 10, and a first plate-frame filter press 11. The feed end of the first reactor 6 is connected to the output end of the advanced oxidation device 5 via a pipeline. The liquid inlet end of the first reactor 6 is connected to the output end of the first extractant storage tank 2 via a pipeline. The discharge end of the first reactor 6 is connected to the feed end of the first centrifuge 9 via a pipeline. The discharge end of the first centrifuge 9 is connected to the discharge end of the first vacuum separator 10 via a pipeline. The discharge end of the first vacuum separator 10 is connected to the feed end of the first plate-frame filter press 11 via a pipeline. The liquid outlet pipes of the first centrifuge 9, the first vacuum separator 10, and the first plate-frame filter press 11 are all connected to the first extractant storage tank 2 via pipelines.

[0024] The catalyst recovery and regeneration system adopts a non-oxidizing and single organic solvent extraction method. The catalyst recovery and regeneration method includes the following steps: S1: Weigh 100g of waste Cu-Bi catalyst and add it into the first reaction kettle 6; S2: Add 200 mL of methanol to the first reaction kettle 6 and stir evenly to ensure that the spent Cu-Bi catalyst is fully in contact with the methanol; S3: Heat the first reactor 6 to 30°C, maintain normal pressure, and stir to react for 2 hours; then increase the temperature to 40°C, increase the pressure to 0.2 MPa, and continue stirring to react for 2 hours; S4: After the reaction is completed, the reaction mixture is centrifuged in a first centrifuge 9 at a centrifugal speed of 4000 rpm to separate the organic phase and the solid phase; S5: distilling the separated organic phase to remove the solvent to obtain a solid powder rich in Cu-Bi active components; S6: The regenerated spent Cu-Bi catalyst was mixed with a fresh Cu-Bi catalyst in a mass ratio of 1:9. The regenerated catalyst was used to produce 1,4-butanediol via the acetylene-formaldehyde process. The reaction conditions were: temperature 90°C, pressure 0.5 MPa, and reaction time 6 hours. Testing showed a formaldehyde conversion rate of 84% and a 1,4-butanediol selectivity of 86%.

[0025] The catalyst recovery and regeneration system adopts low-temperature plasma oxidation and single solvent extraction. The catalyst recovery and regeneration method includes the following steps: S1: Weigh 250g of spent Cu-Bi catalyst and disperse it in the reaction water tank of the low-temperature plasma oxidation device (125g / L); S2: Control the reaction temperature during oxidation to 65°C, continue oxidation for 3 hours, and then enter the first reactor 6; S3: Add 250 mL of ethanol to the first reaction kettle 6 and stir evenly to allow the catalyst to fully contact with the solvent; S4: Heat the first reactor 6 to 30°C, maintain normal pressure, and stir to react for 2 hours; S5: After the reaction is completed, the mixture is centrifuged in a first centrifuge 9 at a centrifugal speed of 4000 rpm to separate the organic phase and the solid phase; S6: distilling the separated organic phase to remove the solvent to obtain a solid powder rich in Cu-Bi active components; S7: The regenerated spent Cu-Bi catalyst was mixed with a fresh Cu-Bi catalyst in a mass ratio of 1:9. The regenerated catalyst was used to produce 1,4-butanediol via the acetylene-formaldehyde process. The reaction conditions were: temperature 90°C, pressure 0.75 MPa, and reaction time 6.5 hours. Testing showed a formaldehyde conversion rate of 89% and a 1,4-butanediol selectivity of 91%.

[0026] Example 2 Example 2 differs from Example 1 in that the catalyst recovery and regeneration method is different. This example also includes a second-stage recovery subsystem, which includes a second extractant storage tank 3, a second reactor 7, a second centrifuge 12, a second vacuum separator 13, and a second plate-frame filter press 14. The feed end of the second reactor 7 is connected to the discharge end of the first plate-frame filter press 11 via a first delivery pipeline. The liquid inlet end of the second reactor 7 is connected to the output end of the second extractant storage tank 3 via a pipeline. The discharge end of the second reactor 7 is connected to the feed end of the second centrifuge 12 via a pipeline. The discharge end of the second centrifuge 12 is connected to the discharge end of the second vacuum separator 13 via a pipeline. The discharge end of the second vacuum separator 13 is connected to the feed end of the second plate-frame filter press 14 via a pipeline. The liquid outlet pipes of the second centrifuge 12, the second vacuum separator 13, and the second plate-frame filter press 14 are all connected to the second extractant storage tank 3 via pipelines. The first delivery pipeline is preferably a screw conveyor.

[0027] The catalyst recovery and regeneration system adopts low-temperature plasma oxidation and cascade extraction. The catalyst recovery and regeneration method includes the following steps: S1: Weigh 200g of spent Cu-Bi catalyst and disperse it in the reaction water tank of the low-temperature plasma oxidation device (100g / L); S2: Control the reaction temperature during oxidation to 60°C, continue oxidation for 2.5 hours, and then enter the first reactor 6; S3: Add 350 mL of methanol to the first reaction kettle 6 and stir evenly to ensure that the spent Cu-Bi catalyst is fully in contact with the methanol; S4: Heat the first reactor 6 to 40°C, maintain normal pressure, stir and react for 2.5h, pass through the first centrifugal separator 9 and the first vacuum separator 10 and The first plate and frame filter press 11 performs solid-liquid separation with a vacuum degree of 0.08 MPa and a plate and frame pressure of 4 MPa to obtain an organic phase and a first solid phase; S5: The solid phase generated in the first reactor 6 is transferred to the second reactor 7. 400 mL of a mixture of petroleum ether and acetone (volume ratio 1:1) is added to the filtered waste Cu-Bi catalyst and stirred evenly to allow the waste Cu-Bi catalyst to fully contact the solvent. The temperature in the second reactor 7 is raised to 40°C and the pressure is raised to 0.3 MPa. The reaction is continued with stirring for 2 h. S6: After the reaction is completed, the mixture generated by the reaction in the second reactor 7 is passed through a second centrifugal separator 12, a second vacuum separator 13, and a second plate and frame filter press 14 for solid-liquid separation, with a vacuum degree of 0.08 MPa and a plate and frame pressure of 4 MPa to obtain an organic phase and a second solid phase. The second solid phase is filtered to obtain the regenerated spent Cu-Bi catalyst; S7: The regenerated spent Cu-Bi catalyst was mixed with fresh Cu-Bi catalyst in a mass ratio of 1:9 and used in the production of 1,4-butanediol via the acetylene-formaldehyde process. The reaction conditions were: 80°C, 0.45 MPa, and 8 hours. Testing showed a formaldehyde conversion rate of 92% and a 1,4-butanediol selectivity of 95%.

[0028] Example 3 Example 3 differs from Example 2 in that the catalyst recovery and regeneration method is different. This example also includes a third-stage recovery subsystem, which includes a third extractant storage tank 4, a third reactor 8, a third centrifuge 15, a third vacuum separator 16, and a third plate-frame filter press 17. The feed end of the third reactor 8 is connected to the discharge end of the second plate-frame filter press 14 via a pipeline. The liquid inlet of the third reactor 8 is connected to the output end of the third extractant storage tank 4 via a second delivery pipeline. The discharge end of the third reactor 8 is connected to the feed end of the third centrifuge 15 via a pipeline. The discharge end of the third centrifuge 15 is connected to the discharge end of the third vacuum separator 16 via a pipeline. The discharge end of the third vacuum separator 16 is connected to the feed end of the third plate-frame filter press 17 via a pipeline. The liquid outlet pipes of the third centrifuge 15, the third vacuum separator 16, and the third plate-frame filter press 17 are all connected to the third extractant storage tank 4 via pipelines. The second delivery pipeline is preferably a screw conveyor. The first reactor 6, the second reactor 7, and the third reactor 9 are preferably ozone catalytic reaction towers. The first centrifuge 9, the second centrifuge 12, and the third centrifuge 15 are preferably horizontal spiral discharge sedimentation centrifuges, available from Xiangtan Centrifuge Co., Ltd., LW series. The first vacuum separator 10, the second vacuum separator 13, and the third vacuum separator 16 are preferably vacuum ceramic filters, available from Yantai Tongxing Industrial Group, TC series. The first plate and frame filter press 11, the second plate and frame filter press 14, and the third plate and frame filter press 17 are preferably ultra-high pressure plate and frame filter presses, available from Zhengzhou Dingsheng, model CGYB-2000.

[0029] The catalyst recovery and regeneration system adopts superoxide oxidation and cascade extraction. The catalyst recovery and regeneration method includes the following steps: S1: Weigh 150g of waste Cu-Bi catalyst and disperse it in the reaction water tank of the superoxide oxidation device. The concentration of the waste Cu-Bi catalyst is 150g / L. S2: Control the reaction temperature of the superoxide oxidation device to 50°C during oxidation, continue oxidation for 2.5 hours, and then enter the first reactor 6; S3: Add 300 mL of petroleum ether to the first reactor 6 and stir evenly to allow the waste Cu-Bi catalyst to fully contact with the petroleum ether. Heat the first reactor 6 to 25°C, maintain normal pressure, and stir to react for 1 hour. S4: The primary mixture generated in the first reactor 6 is subjected to solid-liquid separation by a first centrifugal separator 9, a first vacuum separator 10, and a first plate-and-frame filter press 11 to obtain a first organic phase and a first solid phase. The vacuum degree is 0.08 MPa and the plate-and-frame pressure is 4 MPa. S5: After filtering the first solid phase in step S4, transfer it to the second reactor 7, add 300 mL of toluene to the second reactor 7, stir evenly to allow the catalyst to fully contact with the solvent, raise the temperature in the second reactor 7 to 55° C. and the pressure to 0.25 MPa, and continue stirring to react for 2 hours; S6: After the reaction is completed, the secondary mixture produced in the second reactor 7 is passed through a second centrifugal separator 12, a second vacuum separator 13, and a second plate and frame filter press 14 for solid-liquid separation, with a vacuum degree of 0.08 MPa and a plate and frame pressure of 4 MPa to obtain a second organic phase and a second solid phase; S7: After filtering the second solid phase, transfer it to the third reactor 8, add 300 mL of methanol to the third reactor 8, stir evenly to allow the catalyst to fully contact with the solvent, set the temperature of the third reactor 8 to 30° C. and the pressure to normal pressure, and continue stirring and reacting for 2 hours; S8: After the reaction is completed, the tertiary mixture produced in the third reactor 8 is passed through a third centrifugal separator 15, a third vacuum separator 16 and a third plate and frame filter press 17 for solid-liquid separation, with a vacuum degree of 0.08 MPa and a plate and frame pressure of 4 MPa to obtain a third organic phase and a third solid phase. The third solid phase is filtered to obtain a regenerated spent Cu-Bi catalyst; S9: The regenerated spent Cu-Bi catalyst was mixed with a new catalyst in a mass ratio of 1:9 and used in the production of 1,4-butanediol via the acetylene-formaldehyde process. The reaction conditions were: 85°C, 0.4 MPa, and 7 hours. Testing showed a formaldehyde conversion rate of 92% and a 1,4-butanediol selectivity of 96%.

[0030] Working process and principle: The working principles of the second-level recovery subsystem and the third-level recovery subsystem are the same as those of the first-level recovery subsystem. Taking the working principle of the second-level recovery subsystem as an example, the waste Cu-Bi catalyst is transported from the batching bin 1 to the advanced oxidation device 5, enters the reaction water tank of the advanced oxidation device 5 for oxidation, and then enters the reactor 6 for extraction. After extraction, it passes through the first centrifugal separator 9, the first vacuum separator 10 and the first plate and frame filter press 11 to realize centrifugal separation, vacuum separation and plate and frame filter press separation in sequence to obtain solid and liquid materials. The solid material can enter the reactor of the next-level recovery subsystem for re-extraction, and the liquid material is recovered to the extractant storage tank for reuse. The first-level recovery subsystem, the second-level recovery subsystem and the third-level recovery subsystem cooperate to realize the cascade extraction operation of the catalyst.

Claims

1. A catalyst recovery and regeneration system, characterized in that: including an advanced oxidation unit (5) and a first stage recovery subsystem; The first-stage recovery subsystem includes a first extractant storage tank (2), a first reaction kettle (6), a first centrifugal separator (9), a first vacuum separator (10) and a first plate-and-frame filter press (11); The feed end of the first reactor (6) is connected to the output end of the advanced oxidation device (5) through a pipeline, the liquid inlet end of the first reactor (6) is connected to the output end of the first extractant storage tank (2) through a pipeline, the discharge end of the first reactor (6) is connected to the feed end of the first centrifugal separator (9) through a pipeline, the discharge end of the first centrifugal separator (9) is connected to the discharge end of the first vacuum separator (10) through a pipeline, the discharge end of the first vacuum separator (10) is connected to the feed end of the first plate-frame filter press (11) through a pipeline, and the liquid outlet pipes of the first centrifugal separator (9), the first vacuum separator (10) and the first plate-frame filter press (11) are all connected to the first extractant storage tank (2) through a pipeline.

2. The catalyst recovery and regeneration system according to claim 1, characterized in that: The invention also includes a second-stage recovery subsystem, which includes a second extractant storage tank (3), a second reactor (7), a second centrifugal separator (12), a second vacuum separator (13) and a second plate-frame filter press (14); the feed end of the second reactor (7) is connected to the discharge end of the first plate-frame filter press (11) through a first conveying pipeline, the liquid feed end of the second reactor (7) is connected to the output end of the second extractant storage tank (3) through a pipeline, the discharge end of the second reactor (7) is connected to the feed end of the second centrifugal separator (12) through a pipeline, the discharge end of the second centrifugal separator (12) is connected to the discharge end of the second vacuum separator (13) through a pipeline, the discharge end of the second vacuum separator (13) is connected to the feed end of the second plate-frame filter press (14) through a pipeline, and the liquid outlet pipes of the second centrifugal separator (12), the second vacuum separator (13) and the second plate-frame filter press (14) are all connected to the second extractant storage tank (3) through a pipeline.

3. The catalyst recovery and regeneration system according to claim 2, characterized in that: The invention also includes a third-stage recovery subsystem, which includes a third extractant storage tank (4), a third reactor (8), a third centrifugal separator (15), a third vacuum separator (16) and a third plate-frame filter press (17); the feed end of the third reactor (8) is connected to the discharge end of the second plate-frame filter press (14) through a pipeline, the liquid inlet end of the third reactor (8) is connected to the output end of the third extractant storage tank (4) through a second delivery pipeline, and the third reactor (8) is connected to the third extractant storage tank (4) through a second delivery pipeline. ) is connected to the feed end of the third centrifugal separator (15) through a pipeline, the discharge end of the third centrifugal separator (15) is connected to the discharge end of the third vacuum separator (16) through a pipeline, the discharge end of the third vacuum separator (16) is connected to the feed end of the third plate-frame filter press (17) through a pipeline, and the liquid outlet pipes of the third centrifugal separator (15), the third vacuum separator (16) and the third plate-frame filter press (17) are all connected to the third extractant storage tank (4) through a pipeline.

4. The catalyst recovery and regeneration system according to claim 3, characterized in that: The first conveying pipeline and the second conveying pipeline are both screw conveyors.

5. The catalyst recovery and regeneration system according to claim 3, characterized in that: The advanced oxidation device is a low-temperature plasma oxidation device or a superoxide oxidation device.

6. A method for a catalyst recovery and regeneration system according to any one of claims 1 to 5, characterized in that: The steps include: S1: Weigh a certain amount of spent Cu-Bi catalyst and dissolve it in the reaction water tank of the superoxide oxidation device; S2: Controlling the reaction temperature of the superoxide oxidation device during oxidation, oxidizing the spent Cu-Bi catalyst for a period of time and then transferring it to the first reactor (6); S3: Add 300 mL of petroleum ether to the first reactor (6), stir evenly to allow the catalyst to fully contact the solvent, heat the first reactor (6) to 25°C, maintain normal pressure, and stir to react for 1 hour; S4: The mixture generated in the reactor (6) is subjected to solid-liquid separation by a first centrifugal separator (9), a first vacuum separator (10) and a first plate-and-frame filter press (11) to obtain a first organic phase and a first solid phase; S5: After filtering the first solid phase in step S4, transfer it to the second reactor (7), add 300 mL of toluene to the second reactor (7), stir evenly to allow the catalyst to fully contact with the solvent, raise the temperature in the second reactor (7) to 55°C and the pressure to 0.25 MPa, and continue stirring to react for 2 hours; S6: After the reaction is completed, the mixture produced in the second reactor (7) is passed through a second centrifugal separator (12), a second vacuum separator (13) and a second plate-and-frame filter press (14) for solid-liquid separation to obtain a second organic phase and a second solid phase; S7: After filtering the second solid phase, transfer it to the third reactor (8), add 300 mL of methanol to the third reactor (8), stir evenly to allow the catalyst to fully contact with the solvent, set the temperature of the third reactor (8) to 30°C and the pressure to normal pressure, and continue stirring to react for 2 hours; S8: After the reaction is completed, the mixture produced in the third reactor (8) is subjected to solid-liquid separation by a third centrifugal separator (15), a third vacuum separator (16), and a third plate-and-frame filter press (17) to obtain a third organic matter and a third solid phase, and the third solid phase is filtered to obtain a regenerated spent Cu-Bi catalyst; S9: The regenerated waste Cu-Bi catalyst is mixed with the new catalyst in a mass ratio of 1:9 and used for the reaction of producing 1,4-butanediol by the acetylene aldehyde process.

7. The catalyst recovery and regeneration system according to claim 1, characterized in that: In the step S1, the concentration of the spent Cu-Bi catalyst in the reaction water tank of the superoxide oxidation device is less than 200 g / L.

8. The catalyst recovery and regeneration system according to claim 1, characterized in that: The oxidation temperature in step S2 is 40° C. to 80° C., and the oxidation reaction time is 2 h to 4 h.

9. The catalyst recovery and regeneration system according to claim 1, characterized in that: The temperature of the first reaction kettle (6), the second reaction kettle (7) and the third reaction kettle (8) is 20°C to 80°C, the pressure is normal pressure, the extraction time is 1h to 3h, and the stirring speed is 100rpm to 1000rpm.

10. The catalyst recovery and regeneration system according to claim 1, characterized in that: The centrifugal speed of the first centrifugal separator (9), the second centrifugal separator (12) and the third centrifugal separator (15) is 1000 rpm to 6000 rpm, the vacuum degree of the first vacuum separator (10), the second vacuum separator (13) and the third vacuum separator (16) is 0.05 MPa to 0.1 MPa, and the extrusion separation pressure of the first plate and frame filter press (11), the second plate and frame filter press (14) and the third plate and frame filter press (17) is 1 MPa to 7 MPa.

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