Reactor and system for producing polyether polyol

Abstract

The utility model provides a reactor and system for producing polyether polyol, which comprises a reactor shell, a liquid-liquid-solid three-phase uniform mixing distributor, a fluid stirrer and a feed distributor, the liquid-liquid-solid three-phase uniform mixing distributor is arranged at the top end of the reactor shell, and part of the liquid-liquid-solid three-phase uniform mixing distributor is positioned outside the reactor shell; the fluid stirrer is arranged in the reactor shell and is positioned on the lower side of the liquid-liquid-solid three-phase uniform mixing distributor; the feeding distributor is arranged in the reactor shell and is positioned on the lower side of the fluid stirrer; a discharge opening is formed in the bottom of the reactor shell. A circulating pump and a circulating heat exchanger can be additionally arranged, catalyst slurry is uniformly mixed with circulating fluid through the liquid-liquid-solid three-phase uniform mixing distributor and then uniformly distributed on the whole cross section of the reactor under the action of the fluid stirrer, raw materials are input into the feeding distributor and uniformly distributed on the cross section of the reactor, and the raw materials are uniformly distributed on the cross section of the reactor. And under the effect of density difference, rising and performing countercurrent contact reaction with catalyst slurry.

Description

TECHNICAL FIELD

[0001] The utility model relates to the technical field of polyether polyol production, particularly to a reactor and system for producing polyether polyol. BACKGROUND

[0002] Polyether polyol is an oligomer with ether bond (—R—O—R—) in the main chain and more than two hydroxyl groups (—OH) in the end or side group, and is an organic polymer prepared by polymerization reaction of a starter, ethylene oxide, propylene oxide and butylene oxide in the presence of a catalyst. The most common synthesis process is to use glycerol as a starter and an epoxide (generally PO and EO), and to change the feeding mode (mixed or separate addition), addition ratio, addition sequence and other conditions of PO and EO to produce various specifications of polyether polyol products.

[0003] The synthesis reaction of polyether polyol is a fast reaction. In addition, the active propylene oxide and ethylene oxide have a very high self-polymerization risk, the monomer has high toxicity, and the leakage level is required to be high. In addition, the polyether polyol reaction releases a large amount of heat, which needs to be quickly removed. SUMMARY

[0004] In view of the above-mentioned shortcomings of the prior art, the technical problem to be solved by the utility model is to provide a reactor and system for producing polyether polyol, which is used to solve the problems of large heat release and uneven distribution of catalysts in the reaction process of producing polyether polyol in the prior art, which leads to excessive local reaction.

[0005] To achieve the above-mentioned purpose, the utility model provides a reactor for producing polyether polyol, which comprises a reactor shell, a liquid-liquid-solid three-phase uniform mixing distributor, a fluid agitator and a feeding distributor. The liquid-liquid-solid three-phase uniform mixing distributor is arranged at the top end of the reactor shell and partially located outside the reactor shell. The fluid agitator is arranged in the reactor shell and located below the liquid-liquid-solid three-phase uniform mixing distributor. The feeding distributor is arranged in the reactor shell and located below the fluid agitator. The bottom of the reactor shell is provided with a discharge port.

[0006] Preferably, the reactor shell comprises a main shell, an upper head and a lower head. The main shell is cylindrical. The upper head is fixedly connected to the upper end surface of the main shell, and the liquid-liquid-solid three-phase uniform mixing distributor is arranged on the upper head. The lower head is fixedly connected to the lower end surface of the main shell, and the discharge port is arranged on the lower head.

[0007] Preferably, the liquid-liquid-solid three-phase uniform distribution device comprises a spraying assembly and a uniform mixing assembly, the spraying assembly comprises a spraying pipe body and a jet nozzle, the jet nozzle is arranged at one end of the spraying pipe body, and the other end of the spraying pipe body away from the jet nozzle is connected with a circulating feed pipeline; a connecting hole is formed in the side wall of the spraying pipe body, and a catalyst slurry pipeline is connected to the connecting hole; the top end of the uniform mixing assembly is arranged at the top of an upper head, an upper head through hole is formed in the upper head, the spraying pipe body is inserted into the upper head through hole, and the jet nozzle is located in the uniform mixing assembly; circulating fluid in the circulating feed pipeline and fluid in the catalyst slurry pipeline enter the spraying pipe body together, and are sprayed into the uniform mixing assembly through the jet nozzle.

[0008] Preferably, the uniform mixing assembly is a hollow piece, and the uniform mixing assembly is divided into an inhalation mixing area, an impact uniform mixing area and a diffusion distribution area from top to bottom, the inhalation mixing area is a horn-shaped structure with a large upper end and a small lower end, the impact uniform mixing area is a cylindrical structure, and the diffusion distribution area is a horn-shaped structure with a small upper end and a large lower end; the lower end of the inhalation mixing area has the same diameter as the upper end of the impact uniform mixing area, and the lower end of the impact uniform mixing area has the same diameter as the upper end of the diffusion distribution area.

[0009] Preferably, the diameter of the connection between the spraying pipe body and the circulating feed pipeline is 5-10 times the diameter of the jet nozzle; and the diameter of the impact uniform mixing area is 1.2-1.5 times the diameter of the jet nozzle.

[0010] Preferably, the fluid agitator comprises an agitator main pipe and an agitator short pipe, the agitator main pipe is a circular ring, and the agitator main pipe is fixedly connected to the inner wall of the reactor shell; the agitator main pipe inlet is connected with the circulating feed pipeline; and a plurality of agitator short pipes are arranged obliquely downward on the bottom side wall of the agitator main pipe.

[0011] Preferably, the angle between the tangent direction of the connection between the agitator short pipe and the agitator main pipe and the extension direction of the agitator short pipe is 10-30°; and the diameter of the agitator main pipe is 0.6-0.8 times the diameter of the reactor shell.

[0012] Preferably, the feed distributor is a circular ring, and the feed distributor is fixedly connected to the inner wall of the reactor shell; the inlet of the feed distributor is connected with a raw material feed pipe; and a plurality of feed distributor distribution holes are formed in the bottom side wall of the feed distributor, for uniformly distributing and conveying the raw materials in the raw material feed pipe into the reaction liquid in the reactor.

[0013] Preferably, the feed distributor distribution holes are arranged in two rows, the two rows of feed distributor distribution holes are equidistantly and staggeredly arranged on the lower side wall of the feed distributor, the included angle between the two rows of feed distributor distribution holes is 90-120 degrees, and the diameter of the feed distributor is 0.5-0.9 times the diameter of the reactor shell.

[0014] To achieve the above object or other objects, the utility model relates to a system for producing polyether polyol, adopt the reactor for producing polyether polyol, the system for producing polyether polyol still includes circulating pump, circulating heat exchanger and several pipes, several pipes include circulating pipeline, circulating feed pipeline and discharge pipeline, the circulating feed pipeline includes first circulating feed pipeline, second circulating feed pipeline, the circulating pipeline is connected between the discharge and circulating pump, the circulating pump communicates with circulating heat exchanger, the circulating heat exchanger is connected with the one end of jet pipe body away from jet nozzle through first circulating feed pipeline, the circulating heat exchanger is connected with fluid agitator through second circulating feed pipeline, the circulating heat exchanger is connected with subsequent production equipment through discharge pipeline.

[0015] As described above, the utility model relates to a reactor and system for producing polyether polyol, which has the following beneficial effects:

[0016] The reactor and system for producing polyether polyol can be additionally provided with a circulating pump and a circulating heat exchanger. The catalyst slurry is first uniformly mixed with the circulating fluid through the liquid-liquid-solid three-phase uniform mixing distributor, and then uniformly distributed over the entire cross section of the reactor under the action of the fluid agitator. The raw materials are input from the feed distributor inlet, uniformly distributed over the cross section of the reactor, and react with the catalyst slurry in countercurrent contact under the action of the density difference. The reactor structure in the application has no leakage risk, high mass transfer and heat transfer efficiency, uniform mixing, and can effectively reduce the efficiency of side reactions. BRIEF DESCRIPTION OF DRAWINGS

[0017] Figure 1 is the structural schematic view of the reactor for producing polyether polyol related to the utility model;

[0018] Figure 2 is the structural schematic view of the liquid-liquid-solid three-phase uniform mixing distributor in the reactor for producing polyether polyol related to the utility model;

[0019] Figure 3 is the structural schematic view of the system for producing polyether polyol related to the utility model;

[0020] Figure 4 is the structural schematic view of the feed distributor in the reactor for producing polyether polyol related to the utility model.

[0021] BRIEF DESCRIPTION OF DRAWINGS

[0022] 1. Reactor shell; 101. Upper head; 102. Lower head; 2. Liquid-liquid-solid three-phase homogenizer; 201. Injection assembly; 202. Impact homogenizing zone; 203. Diffusion distribution zone; 204. Suction mixing zone; 3. Fluid agitator; 301. Agitator short tube; 302. Agitator main tube; 4. Feed distributor; 401. Feed distributor distribution hole; 402. Feed distributor inlet; 5. Catalyst slurry pipeline; 6. Raw material feed pipe; 7. Circulation pipeline; 8. Circulation pump; 9. Circulation heat exchanger; 10. Second circulation feed pipeline; 11. First circulation feed pipeline; 12. Discharge pipeline. Detailed Implementation

[0023] The following specific embodiments illustrate the implementation of this utility model. Those skilled in the art can easily understand other advantages and effects of this utility model from the content disclosed in this specification.

[0024] It should be understood that the structures, proportions, sizes, etc., depicted in the accompanying drawings are merely for illustrative purposes to aid those skilled in the art and to facilitate understanding. They are not intended to limit the scope of this invention and therefore have no substantial technical significance. Any modifications to the structure, changes in proportions, or adjustments to size, provided they do not affect the effectiveness or purpose of this invention, should still fall within the scope of the technical content disclosed herein. Furthermore, terms such as "upper," "lower," "left," "right," and "middle" used in this specification are merely for clarity and not intended to limit the scope of this invention. Changes or adjustments to their relative relationships, without substantially altering the technical content, should also be considered within the scope of this invention.

[0025] like Figures 1-4 As shown, this utility model provides a reactor for producing polyether polyols, including a reactor shell 1, a liquid-liquid-solid three-phase homogenizer 2, a fluid agitator 3, and a feed distributor 4. The liquid-liquid-solid three-phase homogenizer 2 is located at the top of the reactor shell 1 and is partially located outside the reactor shell 1; the fluid agitator 3 is located in the reactor shell 1 and is located below the liquid-liquid-solid three-phase homogenizer 2; the feed distributor 4 is located in the reactor shell 1 and is located below the fluid agitator 3; and a discharge port is provided at the bottom of the reactor shell 1.

[0026] The utility model relates to the reactor of production polyether polyol, the initial state has starting liquid and is injected in reactor shell 1. Starting liquid is discharged from the discharge port and is injected into liquid -liquid -solid three phase even mix distributor 2, and starting liquid is mixed with catalyst slurry even in liquid -liquid -solid three phase even mix distributor 2, then enters into starting liquid in reactor shell 1, and fluid agitator 3 stirs circulating fluid, and catalyst slurry is evenly distributed in the liquid surface that fluid agitator 3 stirs. The raw material is input in feed distributor 4, and the raw material evenly spreads on the surface of feed distributor 4 and rises under the action of density difference and countercurrent contact reaction with catalyst slurry.

[0027] Preferably, as shown in Figure 1 、 Figure 3 , the reactor shell 1 includes a main shell, an upper head 101, and a lower head 102. The main shell is cylindrical. The upper head 101 is fixedly connected to the upper end surface of the main shell, and the liquid-liquid-solid three-phase uniform mixing distributor 2 is arranged on the upper head 101. The lower head 102 is fixedly connected to the lower end surface of the main shell, and the discharge port is arranged on the lower head 102. In this embodiment, the reactor shell 1 is a kettle type, the upper head 101 is semicircular or elliptical, and the lower head 102 is conical, semicircular, or elliptical.

[0028] Preferably, as shown in Figure 1 、 Figure 2 , the liquid-liquid-solid three-phase uniform mixing distributor 2 includes a spraying assembly 201 and a uniform mixing assembly. The spraying assembly 201 includes a spraying pipe body and a jet nozzle. The jet nozzle is arranged at the bottom end of the spraying pipe body, and the top end of the spraying pipe body is connected to a circulating feed pipeline. A connecting hole is arranged on the side wall of the spraying pipe body, and a catalyst slurry pipeline 5 is connected to the connecting hole. The top end of the uniform mixing assembly is arranged on the top of the upper head 101. An upper head through hole is arranged on the upper head 101, the spraying pipe body is inserted into the upper head through hole, and the jet nozzle is located in the uniform mixing assembly. The circulating fluid in the circulating feed pipeline and the fluid in the catalyst slurry pipeline 5 enter the spraying pipe body together and are sprayed into the uniform mixing assembly through the jet nozzle. The liquid-liquid-solid three-phase uniform mixing distributor 2 is used for uniformly mixing the circulating fluid and the catalyst slurry, and distributing the diluted mixed catalyst in the liquid surface in the reactor shell 1.

[0029] In this embodiment, the upper head through hole is arranged at the center of the top of the upper head 101. The spraying pipe body is inserted into the upper head through hole. The jet nozzle and the lower half of the spraying pipe body are located inside the reactor shell 1. The upper half of the spraying pipe body is located outside the top end of the reactor shell 1 and is connected to the circulating feed pipeline. The spraying pipe body is sealingly connected to the upper head through hole.

[0030] Preferably, as shown in Figure 2As shown, the uniform mixing assembly is a hollow piece, and the uniform mixing assembly is divided into the suction mixing area 204, the impact uniform mixing area 202 and the diffusion distribution area 203 from top to bottom. The suction mixing area 204 is a horn-shaped structure with a large upper end and a small lower end. The impact uniform mixing area 202 is a cylindrical structure. The diffusion distribution area 203 is a horn-shaped structure with a small upper end and a large lower end. The lower end of the suction mixing area 204 has the same diameter as the impact uniform mixing area 202. The upper end of the diffusion distribution area 203 has the same diameter as the impact uniform mixing area 202.

[0031] Further, in the embodiment, the top end of the uniform mixing assembly is connected to the top of the upper head 101, and the jet nozzle is suspended in the suction mixing area 204. After the circulating fluid and the catalyst slurry in the jet pipe body are sprayed from the jet nozzle, they enter the suction mixing area 204. The high-speed jet flow sprayed from the jet nozzle stirs the buffer liquid in the suction mixing area 204, thereby achieving preliminary mixing.

[0032] Preferably, as shown in Figure 2 , the diameter of the connection between the jet pipe body and the circulating feed pipeline is 5-10 times the diameter of the jet nozzle. The diameter of the impact uniform mixing area 202 is 1.2-1.5 times the diameter of the jet nozzle. As shown in Figure 2 , the inner diameter of the jet nozzle is d1, the inner diameter of the jet pipe body is d3, and d3=(5-10)*d1. The contraction angle of the jet nozzle is 12-20° (for example, the angle a in Figure 2 ). The length of the impact uniform mixing area 202 is h4=50-200mm, the diameter of the impact uniform mixing area 202 is d2, and d2=(1.2-1.5)*d1. The diffusion angle of the diffusion distribution area 203 is 6-12° (for example, the angle b in Figure 2 ).

[0033] Further, the reactor shell 1 contains a reaction liquid mixture, which is the raw material, the catalyst slurry and the polyether polyol generated by the reaction. The above-mentioned mixed liquid is discharged from the discharge port as the circulating fluid, and then is circulated by the circulating feed pipeline. The distance between the bottom end surface of the diffusion distribution area 203 and the liquid level in the reactor shell 1 is 300-1000mm (i.e., h1 in Figure 1 ).

[0034] Preferably, as shown in Figure 1 , the fluid agitator 3 includes an agitator main pipe 302 and agitator short pipes 301. The agitator main pipe 302 is a circular ring, and the agitator main pipe 302 is fixedly connected to the inner wall of the reactor shell 1 through a mounting bracket. The end of the agitator main pipe 302 penetrates the reactor shell 1 and is provided with an agitator main pipe inlet. The agitator main pipe inlet is connected to the circulating feed pipeline. The agitator short pipes 301 are arranged obliquely downward on the outer wall of the agitator main pipe 302. The fluid agitator 3 uses part of the circulating fluid to agitate and mix the fluid in the upper part of the reactor shell 1.

[0035] Preferably, as shown in Figure 1 , the angle between the tangent direction of the connection between the stirring short pipe 301 and the stirring main pipe 302 and the extension direction of the stirring short pipe 301 is 10-30°; the diameter of the stirring main pipe 302 is 0.6-0.8 times the diameter of the reactor shell 1.

[0036] In the embodiment, the fluid stirrer 3 is located below the liquid surface of the starting liquid, at a distance of 100-500mm from the liquid surface (i.e. h2 in Figure 1 ). The position of the fluid stirrer 3 cannot be too high or too low, too high cannot achieve stirring of the liquid in the reactor, too low cannot achieve fast mixing of the circulating fluid mixed with the catalyst slurry sprayed in the mixing assembly and the liquid in the tank, and the problem of local high catalyst concentration will occur. The length of the stirring short pipe 301 is 20-50mm, and the stirring short pipe 301 is inclined downward at an angle of 10-30° with the tangent direction, so that when the circulating fluid is sprayed from the stirring short pipe 301, it is sprayed clockwise or counterclockwise into the liquid in the tank, and the liquid in the tank is stirred with the initial mixed catalyst slurry.

[0037] Preferably, as shown in Figure 1 , Figure 3 , Figure 4 , the feed distributor 4 is a circular ring, and the feed distributor 4 is fixedly connected in the reactor shell 1 through a mounting frame; the feed distributor inlet 402 is connected with the raw material feeding pipe 6; a plurality of feed distributor distribution holes 401 are formed on the feed distributor 4, for conveying and distributing the raw materials in the raw material feeding pipe 6 into the reactor shell 1. The feed distributor 4 is used for uniformly distributing the feed in the reactor shell 1, and improving the mass transfer efficiency of the raw materials.

[0038] Preferably, in the embodiment, the feed distributor distribution holes 401 are arranged in two rows, and the two rows of feed distributor distribution holes 401 are equidistantly and staggeredly distributed on the lower side wall of the feed distributor 4; the angle between the two rows of feed distributor distribution holes 401 is 90-120°; the diameter of the feed distributor 4 is 0.5-0.9 times the diameter of the reactor shell 1. In the embodiment, the hole diameter of the feed distributor distribution hole 401 is 5-15mm. The feed distributor 4 is located at a position 500-1000mm away from the connection between the reactor shell 1 and the lower head 102 (i.e. h3 in Figure 1 ).

[0039] Further, in the embodiment, the raw materials are in a continuous gas phase entraining atomized liquid droplets under the reaction conditions, such as propylene oxide / ethylene oxide; the catalyst slurry is a catalyst slurry containing bimetallic catalyst. In other embodiments, the raw materials and the catalyst slurry can also be other substances.

[0040] To achieve the above-mentioned or other purposes, as shown inFigure 3 The utility model discloses a kind of production polyether polyol's reactor and system, using the above production polyether polyol's reactor, production polyether polyol's system further include circulating pump 8, circulating heat exchanger 9, and several pipelines, several pipelines include circulation pipeline 7, circulating feed pipeline and discharge pipeline 12;Circulating feed pipeline includes first circulating feed pipeline 11, second circulating feed pipeline 10, circulation pipeline 7 is connected between discharge port and circulating pump 8, circulating pump 8 is communicated with circulating heat exchanger 9, circulating heat exchanger 9 is connected with the top of injection pipe body by first circulating feed pipeline 11, circulating heat exchanger 9 is connected with fluid agitator 3 by second circulating feed pipeline 10, circulating heat exchanger 9 is connected with subsequent production equipment by discharge pipeline 12.

[0041] The working principle of the production polyether polyol's reactor and system of the utility model is as follows:

[0042] The present application is the reactor and system scheme of continuous production polyether polyol, catalyst slurry and dilution circulating fluid respectively pass through catalyst slurry pipeline 5 and first circulating feed pipeline 11 and enter into the injection assembly 201 of liquid-liquid solid three-phase uniform mixing distributor 2.Circulating fluid and catalyst slurry form turbulent flow in suction mixing area 204 and preliminarily mix, after preliminary mixing, further microscale mixing is carried out in impact uniform mixing area 202, then evenly drops in starting liquid through diffusion distribution area 203.Catalyst and reaction circulating fluid dilution mixed liquid that are evenly sprayed to the liquid surface in reactor shell 1 are uniformly mixed with liquid in the radial section in the stirring of fluid agitator 3, to avoid local catalyst slurry concentration being too high.Due to the specific structure design of fluid agitator 3, the radial mixing intensity is strengthened, so that catalyst dilution slurry and liquid in kettle are uniformly mixed in the range of 800mm below liquid surface.After uniform mixing, fluid presents piston flow and flows downward, and the feed (mainly in gas phase) that is uniformly raised on the whole reactor section after being distributed by feed distributor 4 countercurrently contacts reaction.

[0043] Kettle reaction liquid is discharged from the bottom of reactor shell 1 through circulation pipeline 7, pressurized by circulating pump 8, cooled by circulating heat exchanger 9, and divided into three ways, one part is discharged as reaction feed through discharge pipeline 12 and enters downstream process, one way enters liquid-liquid solid three-phase uniform mixing distributor 2 through first circulating feed pipeline 11 and dilutes and mixes catalyst slurry, and one way enters fluid agitator 3 through second circulating feed pipeline 10 and is injected into liquid in reactor through stirring short pipe 301 to stir liquid in kettle.

[0044] Kettle reaction liquid is discharged from the bottom of reactor shell 1 through circulation pipeline 7, pressurized by circulating pump 8, cooled by circulating heat exchanger 9, and divided into three ways, one part is discharged as reaction feed through discharge pipeline 12 and enters downstream process, one way enters liquid-liquid solid three-phase uniform mixing distributor 2 through first circulating feed pipeline 11 and dilutes and mixes catalyst slurry, and one way enters fluid agitator 3 through second circulating feed pipeline 10 and is injected into liquid in reactor through stirring short pipe 301 to stir liquid in kettle.

[0045] The utility model relates to the reactor and system of production polyether polyol can connect circulating pump 8, circulating heat exchanger 9 to set up with even mixing subassembly, can make catalyst slurry be diluted and mixed with circulating material quickly, avoid the local excessive reaction caused by catalyst concentration being too high, and the mixing process of catalyst will not be blocked. Set up fluid agitator 3, can make the reactor in the case that there is no mechanical stirring, catalyst slurry and circulating material are evenly distributed on the reaction section of starting liquid, and feeding distributor 4 makes the mixture of raw material ascending and circulating material, catalyst slurry counter current even contact reaction, and reaction heat is diluted by circulating material, can effectively reduce the reaction temperature rise, can ensure POEO not to leak simultaneously, and the reactor inside can reach even mixing of reaction material under the condition that the consistent residence time is kept, and allow high -efficient external circulation heat removal.

[0046] In summary, the utility model effectively overcomes the various shortcomings in the prior art and has high industrial utilization value.

[0047] The above embodiments only exemplarily illustrate the principles and effects of the utility model, and are not used to limit the utility model. Any person skilled in the art can modify or change the above embodiments without departing from the spirit and scope of the utility model. Therefore, all equivalent modifications or changes completed by those skilled in the art without departing from the spirit and technical thought disclosed by the utility model should be covered by the claims of the utility model.

Claims

1. A reactor for producing a polyether polyol, characterized by: The application relates to a reactor shell (1), a liquid-liquid-solid three-phase uniform mixing distributor (2), a fluid stirrer (3) and a feed distributor (4), wherein the liquid-liquid-solid three-phase uniform mixing distributor (2) is arranged at the top end of the reactor shell (1) and partially located outside the reactor shell (1); the fluid stirrer (3) is arranged in the reactor shell (1) and located below the liquid-liquid-solid three-phase uniform mixing distributor (2); the feed distributor (4) is arranged in the reactor shell (1) and located below the fluid stirrer (3); and a discharge port is arranged at the bottom of the reactor shell (1).

2. The reactor for producing polyether polyol according to claim 1, characterized by: The reactor shell (1) comprises a main shell, an upper head (101) and a lower head (102), wherein the main shell is cylindrical; the upper head (101) is fixedly connected to the upper end surface of the main shell, and the liquid-liquid-solid three-phase uniform mixing distributor (2) is arranged on the upper head (101); and the lower head (102) is fixedly connected to the lower end surface of the main shell, and the discharge port is arranged on the lower head (102).

3. The reactor for producing polyether polyol according to claim 1, characterized by: The liquid-liquid-solid three-phase uniform mixing distributor (2) comprises a spraying assembly (201) and a uniform mixing assembly, wherein the spraying assembly (201) comprises a spraying pipe body and a jet nozzle, the jet nozzle is arranged at one end of the spraying pipe body, the end of the spraying pipe body away from the jet nozzle is connected with a circulating feed pipeline, a connecting hole is arranged on the side wall of the spraying pipe body, a catalyst slurry pipeline (5) is connected to the connecting hole, the top end of the uniform mixing assembly is arranged on the bottom surface of the upper head (101), an upper head through hole is arranged on the upper head (101), the spraying pipe body is inserted into the upper head through hole and the jet nozzle is located in the uniform mixing assembly, and the circulating fluid in the circulating feed pipeline and the fluid in the catalyst slurry pipeline (5) enter the spraying pipe body and are sprayed into the uniform mixing assembly through the jet nozzle.

4. A reactor for producing polyether polyols according to claim 3, characterized in that: The uniform mixing assembly is a hollow part, and the uniform mixing assembly is divided into an inhalation mixing area (204), an impact uniform mixing area (202) and a diffusion distribution area (203) from top to bottom, the inhalation mixing area (204) is a horn-shaped part with a large upper end and a small lower end, the impact uniform mixing area (202) is cylindrical, and the diffusion distribution area (203) is a horn-shaped part with a small upper end and a large lower end; the lower end diameter of the inhalation mixing area (204) is the same as the diameter of the impact uniform mixing area (202), and the upper end diameter of the diffusion distribution area (203) is the same as the diameter of the impact uniform mixing area (202).

5. The reactor for producing polyether polyol according to claim 4, characterized by: The diameter of the connection between the spraying pipe body and the circulating feed pipeline is 5-10 times the diameter of the jet nozzle, and the diameter of the impact uniform mixing area (202) is 1.2-1.5 times the diameter of the jet nozzle.

6. The reactor for producing polyether polyol according to claim 1, characterized by: The fluid stirrer (3) comprises a stirrer main pipe (302) and a stirring short pipe (301), the stirrer main pipe (302) is circular and fixed in the reactor, the inlet of the stirrer main pipe (302) is located outside the reactor shell (1) and connected with the circulating feed pipeline, and a plurality of stirring short pipes (301) are arranged on the lower side wall of the stirrer main pipe (302) in a downward direction.

7. A reactor for producing polyether polyols according to claim 6, characterized in that: The included angle between the tangent direction of the connection between the stirring short pipe (301) and the stirring main pipe (302) and the extension direction of the stirring short pipe (301) is 10-30°; the diameter of the stirring main pipe (302) is 0.6-0.8 times the diameter of the reactor shell (1).

8. The reactor for producing polyether polyol according to claim 1, characterized by: The feeding distributor (4) is circular ring-shaped, and is fixedly connected to the side wall of the reactor shell (1); the end of the feeding distributor (4) penetrates through the reactor shell (1) and is provided with a feeding distributor inlet (402), which is connected to the raw material feeding pipe (6); A plurality of feeding distributor distribution holes (401) are formed in the feeding distributor (4) for conveying and uniformly distributing the raw materials in the raw material feeding pipe (6) into the reaction liquid in the reactor.

9. The reactor for producing polyether polyol according to claim 8, characterized by: The feeding distributor distribution holes (401) are arranged in two rows and are symmetrically and staggeredly arranged on the lower side wall of the feeding distributor (4) at equal intervals; the included angle between the two rows of feeding distributor distribution holes (401) is 90-120°; the diameter of the feeding distributor (4) is 0.5-0.9 times the diameter of the reactor shell (1).

10. A system for producing a polyether polyol using the reactor for producing a polyether polyol according to any one of claims 1 to 9, characterized in that: The system for producing polyether polyols further comprises a circulating pump (8), a circulating heat exchanger (9), and a plurality of pipelines, including a circulating pipeline (7), a circulating feeding pipeline, and a discharge pipeline (12); The circulating feeding pipeline comprises a first circulating feeding pipeline (11) and a second circulating feeding pipeline (10); the circulating pipeline (7) is connected between the discharge port and the circulating pump (8); the circulating pump (8) is in communication with the circulating heat exchanger (9); the circulating heat exchanger (9) is connected to the end of the jet pipe body away from the jet nozzle through the first circulating feeding pipeline (11); the circulating heat exchanger (9) is connected to the fluid stirrer (3) through the second circulating feeding pipeline (10); and the circulating heat exchanger (9) is connected to the subsequent production equipment through the discharge pipeline (12).

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