Method and device for reducing content of formaldehyde in olefin epoxidation reaction product

Abstract

The invention discloses a method for reducing the content of formaldehyde in an olefin epoxidation reaction product and a device for a hydrogen peroxide isopropyl benzene ring olefin oxidation reaction. The method for reducing the content of formaldehyde in the olefin epoxidation reaction product comprises the following steps: in the presence of a catalyst, cumyl hydroperoxide material flow and olefin are mixed to carry out epoxidation reaction, and the epoxidation reaction is carried out in stages. According to the method, formaldehyde can be effectively converted into formic acid and other components on the premise that olefin epoxidation reaction indexes are not affected basically, so that the concentration of formaldehyde in a reaction product is remarkably reduced. The method is simple, convenient and easy to operate, and other redundant components cannot be introduced into the reaction product.

Description

Technical Field

[0001] The invention relates to the field of organic chemical technology, in particular to a method for reducing the formaldehyde content in an olefin epoxidation reaction product and a device for olefin epoxidation reaction using cumene hydroperoxide. Background Art

[0002] The use of cumene hydroperoxide to epoxidize olefins to prepare the corresponding epoxides, typically the cumene hydroperoxide method to prepare propylene oxide, has been successfully applied in industry. This process has no by-products and has high reaction selectivity. Cumene hydroperoxide is relatively safe as an oxidant, and the separation and refining steps can also relatively easily obtain high-purity products.

[0003] However, in the operation practice of industrial equipment, it was found that some process pipelines in the refining unit often had blockage problems. Analysis showed that the blockage was polyoxymethylene. The cause could be further traced back to the formaldehyde impurity contained in the epoxidation reaction product. The content only accounted for 100 to 500 ppm of the entire product flow, but it would be enriched in certain areas in the separation and refining unit, thus forming a polymer.

[0004] There are many methods for removing formaldehyde in related fields, such as adsorption and absorption, but it is still a challenge to remove formaldehyde at low cost in industrial scenarios. Practitioners hope to treat it from the source and directly reduce the content of formaldehyde impurities in the epoxidation reaction products, while not causing a significant impact on the technical indicators of the epoxidation reaction, such as the conversion rate of isopropylbenzene hydroperoxide and the selectivity of propylene oxide. Summary of the invention

[0005] In order to solve the above problems existing in the prior art, the present invention provides a method for reducing the formaldehyde content in the olefin epoxidation reaction product. The main feature of the process is that the epoxidation reaction is divided into two stages in series, and each stage can correspond to one or more reactors connected in series or in parallel. In the latter stage reaction in which the concentration of cumene hydroperoxide in the corresponding logistics has dropped to a relatively low level, the reaction temperature is increased to a certain range, and an epoxidation catalyst with an alkaline component is used. In this way, formaldehyde can be effectively converted into formic acid and other components without substantially affecting the olefin epoxidation reaction index, thereby significantly reducing the formaldehyde concentration in the reaction product.

[0006] One of the objects of the present invention is to provide a method for reducing the formaldehyde content in an olefin epoxidation reaction product, comprising mixing a cumene hydroperoxide stream with an olefin for epoxidation in the presence of a catalyst, wherein the epoxidation reaction is carried out in stages.

[0007] According to a preferred embodiment of the present invention, the olefin is a C2-C6 olefin, preferably at least one of ethylene, propylene, butene, butadiene and cyclohexene.

[0008] According to a preferred embodiment of the present invention, the epoxidation reaction is carried out in two stages connected in series, wherein:

[0009] The concentration of cumene hydroperoxide corresponding to the inlet of the front section of the reaction is not limited, and the concentration of cumene hydroperoxide at the inlet of the rear section of the reaction does not exceed 10 wt %.

[0010] According to a more preferred embodiment of the present invention, the concentration of cumene hydroperoxide in the flow at the inlet of the rear stage of the reaction is 0.5 to 2.5 wt %.

[0011] According to a preferred embodiment of the present invention, the catalysts in both the front stage and the back stage of the reaction are epoxidation catalysts, wherein an alkaline component is additionally added to the catalyst in the back stage of the reaction.

[0012] According to a preferred embodiment of the present invention, the epoxidation catalyst is a titanium-based and / or molybdenum-based catalyst.

[0013] According to a more preferred embodiment of the present invention, the epoxidation catalyst is titanate, amorphous TiO 2 / SiO 2 , at least one of a molecular sieve containing framework titanium, molybdic acid, and molybdate.

[0014] According to a preferred embodiment of the present invention, the alkaline component is an oxide or hydroxide of an alkali metal or an alkaline earth metal.

[0015] According to a more preferred embodiment of the present invention, the alkaline component is Na 2 One, two or more of O, CaO, MgO, NaOH and KOH.

[0016] According to a preferred embodiment of the present invention, the amount of the alkaline component added does not exceed 12% of the total weight of the epoxidation catalyst in the latter stage of the reaction, and is preferably 3 to 8 wt%, for example, 3 wt%, 4 wt%, 5 wt%, 6 wt%, 7 wt%, 8 wt%, 9 wt%, 10 wt%, 11 wt%, 12 wt% and a range consisting of any two of the above values.

[0017] According to a preferred embodiment of the present invention, the molar ratio of olefin to cumene hydroperoxide is 5-8.

[0018] According to a preferred embodiment of the present invention, the reaction pressure in the front stage of the reaction is 3-6 MPa.

[0019] According to a preferred embodiment of the present invention, the reaction pressure in the latter stage of the reaction is 3-6 MPa.

[0020] According to a preferred embodiment of the present invention, the reaction temperature in the first stage of the reaction is 80-90°C.

[0021] According to a preferred embodiment of the present invention, the reaction temperature in the latter stage of the reaction is not less than 100°C, preferably 120-150°C, for example, it can be 100°C, 110°C, 120°C, 130°C, 140°C, 150°C and a range consisting of any two of the above values.

[0022] According to a preferred embodiment of the present invention, the formaldehyde content at the outlet of the front stage of the reaction accounts for 20 to 500 ppm of the total mass of the logistics.

[0023] According to a preferred embodiment of the present invention, the formaldehyde content at the outlet of the rear stage of the reaction does not exceed 10 ppm of the total mass of the logistics.

[0024] According to a preferred embodiment of the present invention, both the front stage of the reaction and the back stage of the reaction may correspond to one or more reactors connected in series or in parallel.

[0025] The second object of the present invention is to provide a device for the epoxidation of olefins by cumene hydroperoxide, which is used to carry out the method according to one of the objects of the present invention, comprising a front-stage reaction system and a back-stage reaction system connected in series,

[0026] Front-end reaction system: configured to receive cumene hydroperoxide stream and olefins, and discharge front-end reaction product stream;

[0027] The back-end reaction system is configured to receive the product flow of the front-end reaction and discharge the product flow of the back-end reaction;

[0028] The front-end reaction system and the back-end reaction system include one or more reactors connected in series or in parallel.

[0029] According to a preferred embodiment of the present invention, catalyst beds are provided in the reactors of both the front-end reaction system and the back-end reaction system.

[0030] The present invention divides the epoxidation reaction into two stages connected in series, and each stage can correspond to one or more reactors connected in series or in parallel. In the rear stage reaction corresponding to the concentration of cumene hydroperoxide in the logistics has dropped to a relatively low level, the reaction temperature is increased to a certain range, and an epoxidation catalyst with an alkaline component is used at the same time, so that formaldehyde can be effectively converted into formic acid and other components without substantially affecting the olefin epoxidation reaction index, thereby significantly reducing the formaldehyde concentration in the reaction product. The method is simple, convenient, easy to operate, and other unnecessary components will not be introduced into the reaction product.

[0031] All publications, patent applications, patents and other references mentioned in this specification are incorporated herein by reference. Unless otherwise defined, all technical and scientific terms used in this specification have the meanings conventionally understood by those skilled in the art. In the event of a conflict, the definition in this specification shall prevail.

[0032] When this specification uses the prefix "well-known to those skilled in the art", "prior art" or similar terms to introduce materials, substances, methods, steps, devices or components, etc., the objects introduced by the prefix cover those commonly used in the art when this application is filed, but also include those that are not commonly used at present but will become recognized in the art as being suitable for similar purposes.

[0033] In the context of this specification, except for the contents explicitly described, any matters or items not mentioned are directly applicable to those known in the art without any changes. Moreover, any embodiment described herein can be freely combined with one or more other embodiments described herein, and the technical solutions or technical ideas formed thereby are regarded as part of the original disclosure or original record of the present invention, and should not be regarded as new contents not disclosed or anticipated herein, unless a person skilled in the art considers that the combination is obviously unreasonable.

[0034] The present invention will be further described below by way of examples, but are not limited thereto. DETAILED DESCRIPTION

[0035] The present invention is described in detail below in conjunction with specific embodiments. It is necessary to point out that the following embodiments are only used to further illustrate the present invention and cannot be understood as limiting the scope of protection of the present invention. Some non-essential improvements and adjustments made to the present invention by those skilled in the art based on the contents of the present invention still fall within the scope of protection of the present invention.

[0036] It should also be noted that the various specific technical features described in the following specific embodiments can be combined in any suitable manner without contradiction. To avoid unnecessary repetition, the present invention will not further describe various possible combinations.

[0037] In addition, the various embodiments of the present invention may be arbitrarily combined as long as they do not violate the concept of the present invention. The technical solutions thus formed belong to part of the original disclosure of this specification and also fall within the protection scope of the present invention.

[0038] In the following examples, unless otherwise specified, the experimental methods used are all conventional methods, and the materials and reagents used can be purchased from domestic chemical companies.

[0039] The catalyst used in the examples is CHPO-2000P produced by Sinopec Shanghai Catalyst Company.

[0040] [Example 1]

[0041] The reaction process is divided into two independent stainless steel fixed bed reactors connected in series. The reaction raw materials are propylene and 60wt% cumene hydroperoxide (dissolved in cumene). After mixing, they pass through the catalyst bed of the front reactor and the rear reactor in sequence, wherein propylene: cumene hydroperoxide = 6.0 (molar ratio), the reaction pressure is 5.0 MPa, the front reaction control temperature is 90°C, the reactor is loaded with a titanium olefin epoxidation catalyst (20-40 mesh, 2.0 g), and the concentration of cumene hydroperoxide corresponding to the inlet of the rear reaction is 0.5 wt%, the reaction temperature of the rear-stage reactor is controlled to be 130°C, the reaction pressure is 5.0Mpa, the reactor is loaded with a titanium-based olefin epoxidation mixed catalyst (titanium-based olefin epoxidation catalyst 20-40 mesh, 2.0 g) with added alkaline component (CaO), the added amount of calcium oxide is 5% of the total weight of the titanium-based catalyst in the reactor, the formaldehyde content detected by sampling at the outlet of the front-stage reactor is 200ppm, the formaldehyde content detected by sampling at the outlet of the rear-stage reactor is 15ppm, the conversion rate of isopropylbenzene hydroperoxide is 99.5%, and the selectivity of propylene oxide is 99.1%.

[0042] [Example 2]

[0043] The reaction process is divided into two independent stainless steel fixed bed reactors connected in series. The reaction raw materials are propylene and 60wt% cumene hydroperoxide (dissolved in cumene). After mixing, they pass through the catalyst bed of the front reactor and the rear reactor in sequence, wherein propylene: cumene hydroperoxide = 6.0 (molar ratio), the reaction pressure is 5.0 MPa, the front reaction control temperature is 90°C, the reactor is loaded with a titanium olefin epoxidation catalyst (20-40 mesh, 2.0 g), and the concentration of cumene hydroperoxide corresponding to the inlet of the rear reaction is The reaction temperature of the rear-stage reactor is controlled to be 130°C, the reaction pressure is 5.0Mpa, the reactor is filled with a titanium-based olefin epoxidation mixed catalyst (titanium-based olefin epoxidation catalyst 20-40 mesh, 2.0 g) with an alkaline component (CaO), the amount of calcium oxide added is 8% of the total weight of the titanium-based catalyst, the formaldehyde content detected by sampling at the outlet of the front-stage reactor is 200ppm, the formaldehyde content detected by sampling at the outlet of the rear-stage reactor is 8ppm, the conversion rate of isopropylbenzene hydroperoxide is 99.5%, and the selectivity of propylene oxide is 99.1%.

[0044] [Example 3]

[0045] The reaction process is divided into two independent stainless steel fixed bed reactors connected in series. The reaction raw materials are propylene and 60wt% cumene hydroperoxide (dissolved in cumene). After mixing, they pass through the catalyst bed of the front reactor and the rear reactor in sequence, wherein propylene: cumene hydroperoxide = 6.0 (molar ratio), the reaction pressure is 5.0 MPa, the front reaction control temperature is 90°C, the reactor is loaded with a titanium olefin epoxidation catalyst (20-40 mesh, 2.0 g), and the concentration of cumene hydroperoxide corresponding to the inlet of the rear reaction is The reaction temperature of the rear-stage reactor was controlled at 130°C, the reaction pressure was 5.0 MPa, the reactor was filled with a titanium-based olefin epoxidation mixed catalyst (titanium-based olefin epoxidation catalyst 20-40 mesh, 2.0 g) with an alkaline component (MgO), the amount of magnesium oxide added was 8% of the total weight of the titanium-based catalyst, the formaldehyde content was 200 ppm when sampled at the outlet of the front-stage reactor, and the formaldehyde content was 9 ppm when sampled at the outlet of the rear-stage reactor. The conversion rate of isopropylbenzene hydroperoxide was 99.5%, and the selectivity of propylene oxide was 99.2%.

[0046] [Example 4]

[0047] The reaction process is divided into two independent stainless steel fixed bed reactors connected in series. The reaction raw materials are propylene and 60wt% cumene hydroperoxide (dissolved in cumene). After mixing, they pass through the catalyst bed of the front reactor and the rear reactor in sequence, wherein propylene: cumene hydroperoxide = 6.0 (molar ratio), the reaction pressure is 5.0 MPa, the front reaction control temperature is 90°C, the reactor is loaded with a titanium olefin epoxidation catalyst (20-40 mesh, 2.0 g), and the concentration of cumene hydroperoxide corresponding to the inlet of the rear reaction is 0. .5wt%, the reaction control temperature of the back-end reactor is 130°C, the reaction pressure is 5.0Mpa, the reactor is filled with a titanium-based olefin epoxidation mixed catalyst (titanium-based olefin epoxidation catalyst 20-40 mesh, 2.0 g) with an alkaline component (NaOH), the amount of sodium hydroxide added is 8% of the total weight of the titanium-based catalyst, the formaldehyde content detected by sampling at the outlet of the front-end reactor is 200ppm, the formaldehyde content detected by sampling at the outlet of the back-end reactor is 7ppm, the conversion rate of isopropylbenzene hydroperoxide is 99.5%, and the selectivity of propylene oxide is 99.0%.

[0048] [Example 5]

[0049] The reaction process is divided into two independent stainless steel fixed bed reactors connected in series. The reaction raw materials are propylene and 60wt% cumene hydroperoxide (dissolved in cumene). After mixing, they pass through the catalyst bed of the front reactor and the rear reactor in sequence, wherein propylene: cumene hydroperoxide = 6.0 (molar ratio), the reaction pressure is 5.0Mpa, the front reaction control temperature is 90°C, the reactor is loaded with a titanium olefin epoxidation catalyst (20-40 mesh, 2.0 g), and the concentration of cumene hydroperoxide corresponding to the inlet of the rear reaction is 0.5w t%, the reaction control temperature of the rear-stage reactor is 130°C, the reaction pressure is 5.0Mpa, the reactor is loaded with a titanium-based olefin epoxidation mixed catalyst (titanium-based olefin epoxidation catalyst 20-40 mesh, 2.0 g) with added alkaline components (CaO+MgO), the added amount of metal oxides is 4% of the total weight of the titanium-based catalyst, the formaldehyde content detected by sampling at the outlet of the front-stage reactor is 200ppm, the formaldehyde content detected by sampling at the outlet of the rear-stage reactor is 6ppm, the conversion rate of isopropylbenzene hydroperoxide is 99.5%, and the selectivity of propylene oxide is 99.2%.

[0050] [Example 6]

[0051] The reaction process is divided into two independent stainless steel fixed bed reactors connected in series. The reaction raw materials are propylene and 60wt% cumene hydroperoxide (dissolved in cumene). After mixing, they pass through the catalyst bed of the front reactor and the rear reactor in sequence, wherein propylene: cumene hydroperoxide = 6.0 (molar ratio), the reaction pressure is 5.0Mpa, the front reaction control temperature is 90°C, the reactor is loaded with a titanium olefin epoxidation catalyst (20-40 mesh, 2.0 g), and the concentration of cumene hydroperoxide corresponding to the inlet of the rear reaction is 0.5w t%, the reaction control temperature of the rear-stage reactor is 130°C, the reaction pressure is 5.0Mpa, the reactor is loaded with a titanium-based olefin epoxidation mixed catalyst (titanium-based olefin epoxidation catalyst 20-40 mesh, 2.0 g) with added alkaline components (CaO+MgO), the added amount of metal oxides is 6% of the total weight of the titanium-based catalyst, the formaldehyde content detected by sampling at the outlet of the front-stage reactor is 200ppm, the formaldehyde content detected by sampling at the outlet of the rear-stage reactor is 6ppm, the conversion rate of isopropylbenzene hydroperoxide is 99.5%, and the selectivity of propylene oxide is 99.2%.

[0052] [Example 7]

[0053] The reaction process is divided into two independent stainless steel fixed bed reactors connected in series. The reaction raw materials are propylene and 60wt% cumene hydroperoxide (dissolved in cumene). After mixing, they pass through the catalyst bed of the front reactor and the rear reactor in sequence. The propylene: cumene hydroperoxide = 6.0 (molar ratio), the reaction pressure is 5.0 MPa, the front reaction control temperature is 90°C, the reactor is loaded with a titanium olefin epoxidation catalyst (20-40 mesh, 2.0 g), and the concentration of cumene hydroperoxide corresponding to the inlet of the rear reaction is 0. 5wt%, the reaction temperature of the back-stage reactor is controlled at 150°C, the reaction pressure is 5.0Mpa, the titanium-based olefin epoxidation mixed catalyst (titanium-based olefin epoxidation catalyst 20-40 mesh, 2.0 g) of the alkaline component (CaO+MgO) in the reactor, the added amount of the metal oxide is 4% of the total weight of the titanium-based catalyst, the formaldehyde content detected by sampling at the outlet of the front-stage reactor is 200ppm, the formaldehyde content detected by sampling at the outlet of the back-stage reactor is 5ppm, the conversion rate of isopropylbenzene hydroperoxide is 99.6%, and the selectivity of propylene oxide is 98.5%.

[0054] [Comparative Example 1]

[0055] The reaction process is divided into two independent series-connected two-stage stainless steel fixed-bed reactors, the reaction raw materials are propylene and 60wt% cumene hydroperoxide (dissolved in cumene), which are mixed and successively pass through the catalyst bed of the front-end reactor and the back-end front-end reactor, wherein propylene: cumene hydroperoxide = 6.0 (molar ratio), the reaction pressure is 5.0Mpa, the front-end reaction control temperature is 90°C, the reactor is equipped with a titanium olefin epoxidation catalyst (20-40 mesh, 2.0 grams), the concentration of cumene hydroperoxide corresponding to the reaction back-end inlet is 0.5wt%, the back-end reactor controls the reaction temperature to be 110°C, the reaction pressure is 5.0Mpa, the reactor is equipped with a titanium olefin epoxidation catalyst (20-40 mesh, 2.0 grams). The front-end reactor outlet sampling detection formaldehyde content is 200ppm, the back-end reactor outlet sampling detection formaldehyde content is 50ppm, the hydroperoxide cumene conversion rate is 99.5%, and the propylene oxide selectivity is 99.0%.

[0056] [Comparative Example 2]

[0057] The reaction process is divided into two independent series-connected two-stage stainless steel fixed-bed reactors, the reaction raw materials are propylene and 60wt% cumene hydroperoxide (dissolved in cumene), which pass through the catalyst bed of the front-end reactor and the back-end front-end reactor successively after mixing, wherein propylene: cumene hydroperoxide = 6.0 (molar ratio), the reaction pressure is 5.0Mpa, the front-end reaction is controlled at 90°C, a titanium olefin epoxidation catalyst (20-40 mesh, 2.0 grams) is installed in the reactor, the concentration of cumene hydroperoxide corresponding to the inlet of the back-end reaction is 0.5wt%, the back-end reactor is controlled at a reaction temperature of 130°C, the reaction pressure is 5.0Mpa, a titanium olefin epoxidation catalyst (titanium olefin epoxidation catalyst 20-40 mesh, 2.0 grams) is installed in the reactor, the formaldehyde content detected by sampling at the outlet of the front-end reactor is 200ppm, the formaldehyde content detected by sampling at the outlet of the back-end reactor is 30ppm, the conversion rate of cumene hydroperoxide is 99.5%, and the selectivity of propylene oxide is 99.0%.

[0058] [Comparative Example 3]

[0059] The reaction process is divided into two independent stainless steel fixed bed reactors connected in series. The reaction raw materials are propylene and 60wt% cumene hydroperoxide (dissolved in cumene). After mixing, they pass through the catalyst bed of the front reactor and the rear reactor in sequence, wherein propylene: cumene hydroperoxide = 6.0 (molar ratio), the reaction pressure is 5.0 MPa, the front reaction control temperature is 90°C, the reactor is loaded with a titanium olefin epoxidation catalyst (20-40 mesh, 2.0 g), and the concentration of cumene hydroperoxide corresponding to the inlet of the rear reaction is 0.5 wt%, the reaction temperature of the rear-stage reactor is also controlled to be 90°C, the reaction pressure is 5.0Mpa, the titanium-based olefin epoxidation mixed catalyst (titanium-based olefin epoxidation catalyst 20-40 mesh, 2.0 g) of the alkaline component (CaO+MgO) in the reactor, the added amount of the metal oxide is 4% of the total weight of the titanium-based catalyst, the formaldehyde content detected by sampling at the outlet of the front-stage reactor is 200ppm, the formaldehyde content detected by sampling at the outlet of the rear-stage reactor is 150ppm, the conversion rate of isopropylbenzene hydroperoxide is 99.5%, and the selectivity of propylene oxide is 99.0%.

[0060] [Comparative Example 4]

[0061] The reaction process is a stainless steel fixed bed reactor, the reaction raw materials are propylene and 60wt% cumene hydroperoxide (dissolved in cumene) which are mixed and then passed through a catalyst bed, wherein propylene:cumene hydroperoxide=6.0 (molar ratio), the reaction pressure is 5.0Mpa, the reaction control temperature is 90°C, the reactor is filled with a titanium olefin epoxidation blended catalyst (titanium olefin epoxidation catalyst 20-40 mesh, 2.0 grams) with added alkaline components (CaO+MgO), the added amount of metal oxides is 4% of the total weight of the titanium catalyst, the formaldehyde content detected by sampling at the reactor outlet is 160ppm, the cumene hydroperoxide conversion rate is 99.5%, and the propylene oxide selectivity is 98.8%.

Claims

1. A method for reducing the formaldehyde content in the product of olefin epoxidation reaction, which includes mixing a cumene hydroperoxide logistics with an olefin in the presence of a catalyst to carry out an epoxidation reaction, wherein the epoxidation reaction is carried out in stages.

2. The method according to claim 1, wherein: the olefin is an olefin having 2 to 6 carbon atoms, preferably at least one of ethylene, propylene, butene, butadiene, and cyclohexene.

3. The method according to claim 1, wherein: the epoxidation reaction is carried out in two stages in series, and the concentration of cumene hydroperoxide at the inlet of the latter stage of the reaction does not exceed 10 wt%, preferably 0.5 to 2.5 wt%.

4. The method according to claim 3, wherein: the catalysts in both the former stage and the latter stage of the reaction are epoxidation catalysts, and an alkaline component is added to the catalyst in the latter stage of the reaction.

5. The method according to claim 4, wherein: The epoxidation catalyst is a titanium-based and / or molybdenum-based catalyst, preferably at least one of titanate, amorphous TiO 2 / SiO 2 , molecular sieve containing framework titanium, molybdic acid, and molybdate.

6. The method according to claim 4, wherein: The alkaline component is an oxide or hydroxide of an alkali metal or alkaline earth metal, preferably at least one of Na 2 2O, CaO, MgO, NaOH, and KOH; and / or, the dosage of the alkaline component does not exceed 12% of the total weight of the epoxidation catalyst in the latter stage of the reaction, preferably 3 to 8 wt%.

7. The method according to claim 3, wherein: the reaction temperature in the former stage of the reaction is 80 to 90 °C; and / or, the reaction temperature in the latter stage of the reaction is not lower than 100 °C, preferably 120 to 150 °C.

8. The method according to claim 3, wherein: the formaldehyde content at the outlet of the former stage of the reaction accounts for 20 to 500 ppm of the total mass of the logistics; and / or, the formaldehyde content at the outlet of the latter stage of the reaction does not exceed 10 ppm of the total mass of the logistics.

9. The method according to claim 3, wherein: both the former stage and the latter stage of the reaction can correspond to one or more reactors in series or in parallel.

10. A device for the epoxidation reaction of cumene hydroperoxide with an olefin, which is used to carry out the method according to any one of claims 1 to 9, and includes a former stage reaction system and a latter stage reaction system in series, Former stage reaction system: It is configured to receive a cumene hydroperoxide logistics and an olefin, and discharge the former stage reaction product logistics; Latter stage reaction system: It is configured to receive the former stage reaction product logistics and discharge the latter stage reaction product logistics; The former stage reaction system and the latter stage reaction system include one or more reactors in series or in parallel; preferably, catalyst beds are arranged in the reactors of both the former stage reaction system and the latter stage reaction system.