Method for decomposing spiral-flow type cumyl hydroperoxide

Abstract

The invention discloses a spiral-flow type cumene hydroperoxide (CHP) decomposition reactor and a decomposition method, and the decomposition method comprises the following steps: 1) CHP, a circulating material and desalted water are divided into two streams along a tangent line in a central symmetry manner and enter the top of a conical reactor, and a spiral-flow type flow field is formed in the reactor; (2) intermittently adding resin from the top of the reactor, and rotating along the side wall of the reactor under the action of a spiral-flow type flow field to form a parabolic dense-phase region; and (3) a cylindrical guide cylinder is arranged in the reactor, so that the resin is separated from a reaction product, the reaction product is extracted from the top, and the resin is retained in the reactor. According to the reactor and the decomposition method, the corrosion problem of rear-end equipment caused by concentrated sulfuric acid catalysis can be reduced, fluidization of the resin is realized, the problems of low reaction selectivity, short service life of the resin and the like caused by resin fixed bed catalysis are avoided, meanwhile, replacement of the resin can be realized under the condition of no shutdown, and the production and operation cost is reduced.

Description

Technical Field

[0001] The present invention relates to a method for decomposing peroxide, belonging to the field of reaction technology, and in particular to a method for decomposing cumene hydroperoxide in a swirling flow manner. Background Art

[0002] Cumene hydroperoxide (CHP for short) is an organic peroxide, named because of the peroxide group in the chain segment. In industry, CHP is mostly produced by the peroxidation reaction of cumene with oxygen in the air, and then CHP is decomposed into phenol and acetone under acidic conditions. Phenol and acetone can be used as raw materials for a variety of resins and fibers and are widely used in the industry.

[0003] Industrial CHP is decomposed by acid catalysis. The decomposition process produces a byproduct of dimethylbenzyl alcohol (DMBA). DMBA is further dehydrated to produce alpha-methylstyrene (AMS). AMS is reduced to raw material cumene through rear-end distillation separation and hydrogenation, and then re-peroxidation reaction is carried out. The byproduct AMS produced by CHP decomposition will further polymerize under acidic conditions to form dimers or polymers, forming heavy component tar, reducing the selectivity of the reaction and increasing production costs. Therefore, the decomposition rate of DMBA and the acid concentration after the CHP decomposition reaction need to be controlled during the decomposition process.

[0004] At present, the two main processes used in industry are sulfuric acid catalysis and acid resin catalysis. The concentrated sulfuric acid catalysis process adds 98% concentrated sulfuric acid into the CHP decomposition reactor to provide an acidic environment for CHP decomposition. This process is homogeneous catalysis, with good mixing effect between the catalyst and the material, and high reaction conversion rate and stability. However, sulfuric acid will follow the material into the back-end system, further catalyzing the by-product AMS to generate heavy component tar, reducing the reaction selectivity, and causing corrosion to downstream equipment. The iron ions produced will cause phenol to develop color, affecting product quality. The acid resin catalytic process adds a resin containing a sulfonic acid group into the CHP decomposition reactor to provide an acidic environment for CHP decomposition. The process is a fixed bed heterogeneous catalysis. The acidic solid resin is easy to separate from the material. The by-product AMS is generated under acidic conditions with a short residence time, a small amount of heavy component tar is produced, and the reaction selectivity is high. However, due to the poor dispersibility of the resin, it is easy to cause an imbalance in the local reaction rate in the reactor, a too fast reaction rate, too high local temperature, and an increase in reaction by-products. Long-term operation will also block the resin pores, resulting in resin deactivation. If the reaction rate is too low, CHP enrichment will occur and the reaction stability will decrease. At the same time, the strong oxidizing and swelling properties of the material itself will also destroy the cross-linking structure of the resin itself, resulting in inactivation or shedding of the resin active sites. Summary of the invention

[0005] In view of the defects of the existing technology, the present invention provides a cyclonic flow type cumene hydroperoxide decomposition method, which not only solves the problems of equipment corrosion, product coloration and AMS coking caused by concentrated sulfuric acid catalysis, but also solves the problems of poor resin dispersibility, easy deactivation and complicated replacement, thereby improving the production operation stability and reducing the operation cost.

[0006] In order to achieve the above-mentioned object of the invention, the present invention adopts the following technical solution:

[0007] A cyclonic decomposition method of cumene hydroperoxide comprises the following steps:

[0008] 1) CHP3 and 4 are premixed with desalted water 8 and 9, and then added to the reactor 1 from the top together with the materials in the outer circulation loop of the reactor. The materials in the two circulation loops are sent to the circulation coolers 10 and 11 through product circulation pumps 12 and 13, and after being cooled by the circulation coolers 10 and 11, they enter the reactor 1 tangentially in the horizontal direction in a centrally symmetrical manner, forming a stable cyclonic flow field;

[0009] 2) The reactor 1 is conical and operates with full liquid, wherein the reactor 1 is filled with resin, and under the influence of the cyclonic flow field, a parabolic dense phase area is automatically formed in the conical area at the bottom of the reactor 1, and the fluidization state of the resin can be controlled by adjusting the size of the circulating material flow rate. The top and bottom of the reactor are respectively provided with a resin addition port 5 and a discharge port 2 for replacing the resin during operation. New resin is added to the reactor from the resin addition port 5 through a large funnel, and waste resin is discharged from the reactor by opening the cover plate of the discharge port 2;

[0010] 3) A cylindrical guide tube 14 is installed along the axis inside the reactor 1 to stabilize the internal vortex flow field. At the same time, a baffle 15 is provided at the bottom of the guide tube to improve the separation effect between the resin and the material and realize the separation of the catalytic resin and the reaction product. The final product is discharged from the top axis 6 of the reaction after the residual resin is intercepted by the filter 7.

[0011] In a specific embodiment, the CHP concentration in step 1) is 80-84%, preferably 81-83%; the content of desalted water in the total material is 0.5-3%, preferably 1-2%.

[0012] In a specific embodiment, the ratio of the material flow rate to the feed CHP flow rate in the single circulation loop in step 1) is 10-20:1, preferably 12-18:1, and the reaction temperature is 70-90° C., preferably 75-85° C. In a preferred embodiment, the circulating material in the reactor is divided into two streams. When the heat exchanger has a reduced heat exchange effect due to coking of heavy components and needs to be flushed, a single circulation can achieve CHP feed mixing and reaction heat removal without adjusting the operating load, thereby ensuring reaction stability and safety.

[0013] In a preferred embodiment, the phenol product selectivity of the reactor is controlled at above 98%. When the selectivity is lower than 98%, the feed amount of desalted water needs to be increased to ensure that the phenol product yield is greater than 99.7% and the selectivity is higher than 99.8%.

[0014] In a specific embodiment, in step 2), the ratio of the diameter to the height of the cylindrical part of the conical reactor is 0.5-1:1, and the angle between the conical surface and the horizontal plane is 30-60°.

[0015] In a specific embodiment, the resin catalyst in step 2) is not particularly limited, and a commercial resin catalyst can be selected, such as Lanxiao LXC-101 resin, Kairui KC122C resin, Purolite TC122 resin, and fluorine-containing resin catalyst. From the perspective of improving wear resistance, the fluorine-containing resin catalyst is preferably synthesized by the method provided in patent CN201911351764.4, and the preparation method comprises the following steps:

[0016] 1) (Meth) acrylic acid and a crosslinking agent are reacted at 10-30 kPa and 80-90° C. for 3-6 hours;

[0017] 2) adding styrene and 1,3,5-trifluoro-2-vinylbenzene to the reaction solution of step 1), and adding a porogen, wherein the molar ratio of styrene, 1,3,5-trifluoro-2-vinylbenzene, (meth)acrylic acid and crosslinking agent is 50-80:20-50:1-8:1-8, and performing suspension polymerization in the presence of a free radical initiator to obtain macroporous styrene-based random crosslinked copolymer resin mother balls;

[0018] 3) swelling the resin mother ball with a solvent, and adding concentrated sulfuric acid to sulfonate the resin mother ball to obtain the resin catalyst;

[0019] Wherein, the cross-linking agent is a silane coupling agent shown in formula (I):

[0020]

[0021] Where m is 1-30.

[0022] For other process conditions and process steps in the preparation process of the resin catalyst, reference is made to the contents provided in CN201911351764.4.

[0023] In a specific embodiment, the filling volume of the resin in step 2) accounts for 0.5-10% of the total volume of the reactor, the resin exchange capacity is 5-8 eq / kg, and the average particle size is 0.5-1.2 mm.

[0024] In a preferred embodiment, when the CHP concentration at the outlet of the reactor is higher than 1%, the resin in the reactor needs to be replaced to ensure the conversion rate of CHP decomposition, and the resin is added from the upper part of the reactor, the addition port is located between the guide tube and the outer wall of the reactor, and the deactivated resin is discharged from the bottom of the conical reactor at the same time until the CHP concentration at the outlet of the reactor is lower than 0.1%, and the filling volume of the resin is kept unchanged during the process.

[0025] In a specific embodiment, the ratio of the diameter of the cylindrical draft tube in step 3) to the diameter of the reactor is 0.4-0.6:1, and the ratio of its height to the height of the straight pipe section of the reactor is 0.8-1:1.

[0026] In a specific embodiment, a baffle is provided at the bottom of the cylindrical draft tube in step 3), the baffle is 30-60° with the horizontal plane, and extends obliquely downward toward the reactor wall, and the ratio of the length of a single baffle to the diameter of the draft tube is 0.01-0.05:1.

[0027] In a specific embodiment, the filter in step 3) has a filtration pore size of 0.4-1 mm, which is used to intercept broken resin particles.

[0028] Compared with the prior art, the beneficial effects of the present invention are mainly reflected in the following aspects:

[0029] 1. Solve the corrosion problem of back-end equipment caused by concentrated sulfuric acid catalysis. Through the fluidization of resin, avoid the low reaction selectivity and short resin life caused by fixed bed catalysis. At the same time, the resin can be replaced without stopping the production, which increases the production operation cycle.

[0030] 2. The design of two circulation loops and the guide tube can provide a stable cyclonic flow field for the reactor, while ensuring the separation of resin and reaction products, and facilitating the uniform mixing of feed and the removal of reaction heat, thereby improving reaction stability and safety.

[0031] 3. By adding a certain amount of desalted water, the formation of the intermediate product α-methylstyrene is inhibited, the formation and coking rate of the heavy components cumylphenol and α-methylstyrene dimer in the CHP decomposition process are reduced, and the generated heavy components are prevented from clogging the resin pores.

[0032] 4. A baffle is designed at the bottom of the cylindrical guide tube, which extends obliquely downward toward the reactor wall, thereby improving the solid-liquid separation effect, avoiding resin entrainment in the reaction product, and achieving efficient separation of the catalytic resin.

[0033] 5. After the reaction product leaves the reactor, it is filtered through a filter to fully remove the entrained resin powder to prevent the resin from clogging and corroding the rear-end pipeline. By selecting a resin containing fluorine, the wear resistance of the resin itself can be effectively improved to avoid the generation of resin powder. BRIEF DESCRIPTION OF THE DRAWINGS

[0034] Figure 1 The figure is a schematic diagram of the process flow of the cyclonic cumene hydroperoxide decomposition reactor and the decomposition method of the present invention,

[0035] Among them, 1 is a decomposition reactor, 2 is a catalyst discharge port, 3 is a reactor feed, 4 is a reactant feed, 5 is a catalyst addition port, 6 is a decomposition product outlet, 7 is a basket filter, 8 is a desalted water addition port, 9 is a desalted water addition port, 10 is a circulating cooler, 11 is a circulating cooler, 12 is a product circulating pump, and 13 is a product circulating pump;

[0036] Figure 2 It is a top view of a cyclonic cumene hydroperoxide decomposition reactor;

[0037] Figure 3 It is a bottom view of the cyclonic hydroperoxide cumene decomposition reactor. DETAILED DESCRIPTION

[0038] In order to better understand the technical solution of the present invention, the following examples will further illustrate the method provided by the present invention, but the present invention is not limited to the listed examples, and should also include any other known changes within the scope of the claims of the present invention.

[0039] Raw materials and sources:

[0040] The reactants used in this patent come from Wanhua Chemical Co., Ltd.'s bisphenol A plant with an annual production capacity of 480,000 tons, and the sulfuric acid and desalted water come from the supporting public works.

[0041] Preparation of catalyst resin

[0042] The preparation method of the resin catalyst is as follows:

[0043] 1) reacting acrylic acid and a cross-linking agent at 10 and 80°C for 6 h to obtain a resin with a particle size of 1.2 mm, wherein the molar ratio of acrylic acid to the cross-linking agent is 1:1;

[0044] 2) Add styrene and 1,3,5-trifluoro-2-vinylbenzene to the reaction solution, control the fluorine content, and react at 200 and 80° C. for 6 hours to obtain macroporous styrene-based random cross-linked copolymer resin mother balls, wherein the molar ratio of styrene, 1,3,5-trifluoro-2-vinylbenzene, (meth)acrylic acid and cross-linking agent is 50:20:1:1,

[0045] 3) swelling the resin mother ball with toluene solvent, adding an amount of 150% of the total weight of styrene and 1,3,5-trifluoro-2-vinylbenzene, and sulfonating the resin mother ball with sulfuric acid at a concentration of 0.7% to obtain a resin catalyst with an exchange capacity of 6 eq / kg;

[0046] Test method:

[0047] The resin strength test is carried out according to GB / T 12598-90, the resin exchange capacity is tested according to GB / T5476-92013, and the resin particle size is tested according to GB / T 5758-2001.

[0048] Embodiment 1:

[0049] like Figure 1 As shown, 84% concentration CHP solution from the peroxidation and concentration unit is added into two circulation loops of the CHP decomposition reactor in two streams, and desalted water is added during the process to maintain the desalted water content in the circulation loop at 3%, the circulation volume to feed ratio is 10:1, and the reaction temperature is 90°C.

[0050] After the circulating material enters the reactor, a cyclonic flow field is formed. The ratio of the diameter to the height of the cylindrical part of the reactor is 0.5:1, the angle between the conical part and the horizontal plane is 45°, the ratio of the diameter of the guide tube to the diameter of the reactor is 0.5:1, the ratio of the height to the height of the reactor is 0.8:1, the angle between the outward turning angle of the guide tube and the horizontal plane is 30°, and the ratio of the turning angle length to the diameter of the reactor is 0.01:1.

[0051] The resin used in this embodiment has a diameter of 1.2 mm, an exchange capacity of 6 eq / kg, a filling amount of 5%, a filter pore size of 1 mm, a controlled outlet CHP content of 0.1%, a CHP yield of 99.7%, and a selectivity of 99.82%.

[0052] Embodiment 2:

[0053] like Figure 1 As shown, 80% concentration CHP solution from the peroxidation and concentration unit is added into two circulation loops of the CHP decomposition reactor in two streams, and desalted water is added during the process to maintain the water content in the circulation loop at 1.75%, the circulation volume to feed ratio is 20:1, and the reaction temperature is 85°C.

[0054] After the circulating material enters the reactor, a cyclonic flow field is formed. The ratio of the diameter to the height of the cylindrical part of the reactor is 0.75:1, the angle between the conical part and the horizontal plane is 30°, the ratio of the diameter of the guide tube to the diameter of the reactor is 0.4:1, the ratio of the height to the height of the reactor is 0.9:1, the angle between the outward turning angle of the guide tube and the horizontal plane is 45°, and the ratio of the turning angle length to the diameter of the reactor is 0.05:1.

[0055] The resin used in this embodiment has a diameter of 1.2 mm, an exchange capacity of 6 eq / kg, a filling amount of 0.5%, a filter pore size of 0.4 mm, a controlled outlet CHP content of 0.5%, a CHP yield of 99.71%, and a selectivity of 99.8%.

[0056] Embodiment 3:

[0057] like Figure 1 As shown, 82% CHP solution from the peroxidation and concentration unit is added into two circulation loops of the CHP decomposition reactor in two streams, and desalted water is added during the process to maintain the water content in the circulation loop at 0.5%, the circulation volume to feed ratio is 15:1, and the reaction temperature is 70°C.

[0058] After the circulating material enters the reactor, a cyclonic flow field is formed. The ratio of the diameter to the height of the cylindrical part of the reactor is 1:1, the angle between the conical part and the horizontal plane is 60°, the ratio of the diameter of the guide tube to the diameter of the reactor is 0.4:1, the ratio of the height to the height of the reactor is 1:1, the angle between the outward turning angle of the guide tube and the horizontal plane is 60°, and the ratio of the turning angle length to the diameter of the reactor is 0.03:1.

[0059] The resin used in this embodiment has a diameter of 1.2 mm, an exchange capacity of 6 eq / kg, a filling amount of 10%, a filter pore size of 0.7 mm, a controlled outlet CHP content of 1%, a CHP yield of 99.6%, and a selectivity of 99.78%.

[0060] Example 4

[0061] like Figure 1 As shown, 83% concentration CHP solution from the peroxidation and concentration unit is added into two circulation loops of the CHP decomposition reactor in two streams, and desalted water is added during the process to maintain the water content in the circulation loop at 2.5%, the circulation volume to feed ratio is 18:1, and the reaction temperature is 80°C.

[0062] After the circulating material enters the reactor, a cyclonic flow field is formed. The ratio of the diameter to the height of the cylindrical part of the reactor is 0.9:1, the angle between the conical part and the horizontal plane is 50°, the ratio of the diameter of the guide tube to the diameter of the reactor is 0.6:1, the ratio of the height to the height of the reactor is 1:1, the angle between the outward turning angle of the guide tube and the horizontal plane is 50°, and the ratio of the turning angle length to the diameter of the reactor is 0.04:1.

[0063] The resin used in this embodiment has a diameter of 1.2 mm, an exchange capacity of 6 eq / kg, a filling amount of 8%, a filter pore size of 0.9 mm, a controlled outlet CHP content of 0.7%, a CHP yield of 99.84%, and a selectivity of 99.73%.

[0064] Example 5

[0065] like Figure 1 As shown, 81% concentration CHP solution from the peroxidation and concentration unit is added into two circulation loops of the CHP decomposition reactor in two streams, and desalted water is added during the process to maintain the water content in the circulation loop at 1.5%, the circulation volume to feed ratio is 12:1, and the reaction temperature is 75°C.

[0066] After the circulating material enters the reactor, a cyclonic flow field is formed. The ratio of the diameter to the height of the cylindrical part of the reactor is 0.6:1, the angle between the conical part and the horizontal plane is 40°, the ratio of the diameter of the guide tube to the diameter of the reactor is 0.5:1, the ratio of the height to the height of the reactor is 0.8:1, the angle between the outward turning angle of the guide tube and the horizontal plane is 40°, and the ratio of the turning angle length to the diameter of the reactor is 0.02:1.

[0067] The resin used in this embodiment has a diameter of 1.2 mm, an exchange capacity of 6 eq / kg, a filling amount of 6%, a filter pore size of 0.5 mm, a controlled outlet CHP content of 0.3%, a CHP yield of 99.8%, and a selectivity of 99.7%.

[0068] Example 6

[0069] like Figure 1 As shown, 80% concentration CHP solution from the peroxidation and concentration unit is added into two circulation loops of the CHP decomposition reactor in two streams, and desalted water is added during the process to maintain the water content in the circulation loop at 1.75%, the circulation volume to feed ratio is 20:1, and the reaction temperature is 85°C.

[0070] After the circulating material enters the reactor, a cyclonic flow field is formed. The ratio of the diameter to the height of the cylindrical part of the reactor is 0.75:1, the angle between the conical part and the horizontal plane is 30°, the ratio of the diameter of the guide tube to the diameter of the reactor is 0.4:1, the ratio of the height to the height of the reactor is 0.9:1, the angle between the outward turning angle of the guide tube and the horizontal plane is 45°, and the ratio of the turning angle length to the diameter of the reactor is 0.05:1.

[0071] This comparative example uses fluorine-free Lanxiao LXC-101 resin, with a resin diameter of 1.2 mm, a resin exchange capacity of 6 eq / kg, a resin filling amount of 0.5%, a filter pore size of 0.7 mm, a controlled outlet CHP content of 1%, a CHP yield of 99.65%, and a selectivity of 99.80%. After running for 3 months, the sulfonate shedding rate was 20%, and the filter intercepted and crushed resin accounted for 25% of the total added amount.

[0072] Comparative Example 1

[0073] like Figure 1 As shown, 82% CHP solution from the peroxidation and concentration unit is added into two circulation loops of the CHP decomposition reactor in two streams, and desalted water is added during the process to maintain the water content in the circulation loop at 0.1%, the circulation volume and feed ratio is 15:1, and the reaction temperature is 70°C.

[0074] After the circulating material enters the reactor, a cyclonic flow field is formed. The ratio of the diameter to the height of the cylindrical part of the reactor is 1:1, the angle between the conical part and the horizontal plane is 60°, the ratio of the diameter of the guide tube to the diameter of the reactor is 0.4:1, the ratio of the height to the height of the reactor is 1:1, the angle between the outward turning angle of the guide tube and the horizontal plane is 60°, and the ratio of the turning angle length to the diameter of the reactor is 0.03:1.

[0075] The resin used in this comparative example has a diameter of 1.2 mm, an exchange capacity of 6 eq / kg, a filling amount of 6%, a filter pore size of 0.5 mm, and a water content of 0.1%. The CHP yield is 97.8% and the selectivity is 96.7%.

[0076] Comparative Example 2

[0077] like Figure 1 As shown, 82% concentration CHP solution from the peroxidation and concentration unit is added into two circulation loops of the CHP decomposition reactor in two streams, and desalted water is added during the process to maintain the water content in the circulation loop at 5%, the circulation volume and feed ratio is 15:1, and the reaction temperature is 70°C.

[0078] After the circulating material enters the reactor, a cyclonic flow field is formed. The ratio of the diameter to the height of the cylindrical part of the reactor is 1:1, the angle between the conical part and the horizontal plane is 60°, the ratio of the diameter of the guide tube to the diameter of the reactor is 0.4:1, the ratio of the height to the height of the reactor is 1:1, the angle between the outward turning angle of the guide tube and the horizontal plane is 60°, and the ratio of the turning angle length to the diameter of the reactor is 0.03:1.

[0079] The resin used in this comparative example has a diameter of 1.2 mm, an exchange capacity of 6 eq / kg, a filling amount of 6%, a filter pore size of 0.5 mm, and a water content of 5%. The CHP yield is 96.2% and the selectivity is 95.3%.

[0080] Although the content of the present invention has been described in detail through the above preferred embodiments, it should be appreciated that the above description should not be considered as limiting the present invention. Those skilled in the art will appreciate that, under the guidance of this specification, some modifications or adjustments may be made to the present invention. These modifications or adjustments should also be within the scope defined by the claims of the present invention.

Claims

1. A cyclonic decomposition method of cumene hydroperoxide, characterized in that: The following steps are involved: 1) CHP (3) and (4) are premixed with desalted water (8) and (9), and then added to a reactor (1) from the top together with materials in a circulating loop outside the reactor. The materials in the two circulating loops are sent to circulating coolers (10) and (11) through product circulating pumps (12) and (13), and after being cooled in the circulating coolers (10) and (11), they enter the reactor (1) tangentially in a horizontal direction in a centrally symmetrical manner, forming a stable cyclonic flow field; 2) The reactor (1) is conical and is operated with full liquid, wherein the reactor (1) is filled with resin, and under the influence of the cyclonic flow field, a parabolic dense phase region is automatically formed in the conical region at the bottom of the reactor (1). The top and bottom of the reactor are respectively provided with a resin inlet (5) and a discharge port (2) for replacing the resin during operation. New resin is added to the reactor from the resin inlet (5) through a large funnel, and waste resin is discharged from the reactor by opening the cover plate of the discharge port (2); 3) A cylindrical guide tube (14) is installed along the axis of the reactor (1) to stabilize the internal cyclonic flow field. At the same time, a baffle (15) is provided at the bottom of the guide tube. The final product is discharged from the top axis (6) of the reactor after the residual resin is intercepted by the filter (7).

2. The method for decomposing cumene hydroperoxide according to claim 1, characterized in that: In the step 1), the CHP concentration is 80-84%, preferably 81-83%; the content of desalted water in the total material is 0.5-3%, preferably 1-2%.

3. The method for decomposing cumene hydroperoxide in a cyclonic flow process as claimed in claim 1 or 2, characterized in that: The ratio of the material flow rate to the feed CHP flow rate in the single circulation loop in step 1) is 10-20:1, preferably 12-18:1, and the reaction temperature is 70-90°C, preferably 75-85°C.

4. The cyclonic decomposition method of cumene hydroperoxide according to any one of claims 1 to 3, characterized in that: In the step 2), the ratio of the diameter to the height of the cylindrical part of the conical reactor is 0.5-1:1, and the angle between the conical surface and the horizontal plane is 30-60°.

5. The cyclonic decomposition method of cumene hydroperoxide according to any one of claims 1 to 4, characterized in that: In the step 2), the resin catalyst is selected from Lanxiao LXC-101 resin, Kairui KC122C resin, Purolite TC122 resin, and a fluorine-containing resin catalyst; preferably, the fluorine-containing resin catalyst is synthesized by the method provided in patent CN201911351764.

4.

6. The cyclonic decomposition method of cumene hydroperoxide according to any one of claims 1 to 5, characterized in that: In the step 2), the filling volume of the resin accounts for 0.5-10% of the total volume of the reactor, the resin exchange capacity is 5-8 eq / kg, and the average particle size is 0.5-1.2 mm.

7. The cyclonic decomposition method of cumene hydroperoxide according to any one of claims 1 to 6, characterized in that: The ratio of the diameter of the cylindrical draft tube in step 3) to the diameter of the reactor is 0.4-0.6:1, and the ratio of its height to the height of the straight pipe section of the reactor is 0.8-1:

1.

8. The cyclonic decomposition method of cumene hydroperoxide according to any one of claims 1 to 7, characterized in that: The cylindrical draft tube in step 3) is provided with a baffle at the bottom, the baffle is 30-60 degrees with the horizontal plane, and extends obliquely downward toward the reactor wall. The ratio of the length of a single baffle to the diameter of the draft tube is 0.01-0.05:

1.

9. The cyclonic decomposition method of cumene hydroperoxide according to any one of claims 1 to 8, characterized in that: The filter pore size of the filter in step 3) is 0.4-1 mm.

Images