System and method for enhanced oxidation reaction of ethylbenzene

Abstract

A system and method for an enhanced oxidation reaction of ethylbenzene. The system comprises: an oxidation reactor (1), the oxidation reactor (1) being connected to a gas inlet pipe (4) for inputting a gas-phase raw material and a liquid inlet pipe (11) for inputting a liquid-phase raw material, and a product outlet (101) being provided on the side wall of the oxidation reactor (1); a first enhanced mass transfer unit (3), the first enhanced mass transfer unit (3) being arranged inside the oxidation reactor (1), the gas inlet pipe (4) being connected to the first enhanced mass transfer unit (3), and the gas-phase raw material in the gas inlet pipe (4) being treated by the first enhanced mass transfer unit (3) and then entering the oxidation reactor (1), so as to enhance the mass transfer effect between the gas-phase raw material and the liquid-phase raw material; and a heat exchange pipe (6), an inlet and an outlet of the heat exchange pipe (6) being both communicated with the oxidation reactor (1), the inlet of the heat exchange pipe (6) being arranged below the outlet of the heat exchange pipe (6) in a vertical direction, and a first heat exchanger (7) being arranged on the heat exchange pipe (6). The solution is conducive to improving the reaction efficiency and the product yield of peroxidation reactions of ethylbenzene.

Description

Ethylbenzene intensified oxidation reaction system and method TECHNICAL FIELD The present application relates to the technical field of ethylbenzene oxidation reaction, in particular to an ethylbenzene intensified oxidation reaction system and method. BACKGROUND Propylene oxide-styrene (PO / SM) co-production method, also known as co-oxidation method, is an important chemical production technology. The PO / SM co-production method process technical route mainly uses propylene and ethylbenzene as raw materials to produce propylene oxide and styrene product monomers by co-oxidation method. The process first directly oxidizes ethylbenzene with air or oxygen to generate ethylbenzene hydrogen peroxide (EBHP), and then EBHP and propylene undergo epoxidation reaction under the action of molybdenum-based catalyst to generate methylbenzyl alcohol (phenethyl alcohol) and propylene oxide. The epoxidation reaction liquid is distilled to obtain propylene oxide (PO) product, and the phenethyl alcohol is dehydrated at 260℃ under normal pressure to generate styrene (SM) product. In the related art, ethylbenzene oxidation reaction is usually carried out in multiple (for example, two) non-catalytic, liquid-phase series oxidation reactors. The concentration of EBHP in the reaction product obtained after passing through multiple oxidation reactors is usually only 8-10wt%, and the reaction efficiency is low. Therefore, the present application is proposed. SUMMARY The first object of the present application is to provide an ethylbenzene intensified oxidation reaction system. The reaction system is provided with a first intensified mass transfer unit in the oxidation reactor and a heat exchange pipeline in communication with the oxidation reactor, which helps to improve the reaction efficiency and product yield of ethylbenzene peroxide reaction, and the reaction product The concentration of ethylbenzene peroxide in the reaction product is high, which can meet the needs of downstream production. The second object of the present application is to provide an ethylbenzene intensified oxidation reaction method. The method can improve the reaction efficiency and product yield of ethylbenzene peroxide reaction by using the above-mentioned system for ethylbenzene peroxide reaction. In order to achieve the above-mentioned objects of the present application, the following technical solutions are adopted: The present application provides an ethylbenzene intensified oxidation reaction system, comprising: an oxidation reactor, the oxidation reactor being connected with a gas inlet pipeline for inputting gas-phase raw materials and a liquid inlet pipeline for inputting liquid-phase raw materials; a product outlet is arranged on the side wall of the oxidation reactor; a first intensified mass transfer unit, the first intensified mass transfer unit being arranged inside the oxidation reactor, the gas inlet pipeline being connected with the first intensified mass transfer unit, and the gas-phase raw materials in the gas inlet pipeline being treated by the first intensified mass transfer unit and then entering the oxidation reactor to enhance the mass transfer effect between the gas-phase raw materials and the liquid-phase raw materials; a heat exchange pipeline, the inlet and outlet of the heat exchange pipeline being in communication with the oxidation reactor, and the inlet of the heat exchange pipeline being arranged below the outlet of the heat exchange pipeline in the vertical direction; and a first heat exchanger arranged on the heat exchange pipeline. In the related art, the ethylbenzene peroxidation reaction is usually carried out in multiple (for example, two) non-catalytic, liquid-phase series oxidation reactors, and the concentration of EBHP in the reaction product obtained after passing through multiple oxidation reactors is usually only 8-10 wt%. On the one hand, this production system needs to use multiple oxidation reactors, resulting in a relatively large overall occupied space; on the other hand, the concentration of EBHP in the reaction product obtained by this production system is relatively low, the reaction efficiency is low, and due to the relatively low concentration of EBHP, it cannot be directly applied to the downstream (for example, ethylbenzene peroxide hydrogen epoxidation reaction), and usually needs to increase the concentration equipment for further concentration, which further increases the production cost. In addition, the inventors have found through research that the reaction of ethylbenzene oxidation to generate hydrogen peroxide has the characteristics of slow reaction rate, sensitivity to temperature, great influence on product concentration, moderate reaction heat effect, etc., and thus the reactor of this reaction should meet the requirements of large liquid holdup, high heat transfer efficiency, stable operation, easy control of reaction conditions, etc. However, the inventors have further found that the liquid phase backmixing in the reactor (for example, a bubble column reactor) that can meet the requirement of large liquid holdup will seriously affect the reaction selectivity and the control of the reaction, and when the height-diameter ratio of the reactor is large, the coalescence of bubbles will occur, the bubble dispersion effect will become poor, the gas-liquid contact area will be reduced, and the gas-liquid mass transfer efficiency will be affected. In view of the above research, the embodiments of the present application provide an ethylbenzene intensified oxidation reaction system, which only uses one oxidation reactor, can reduce the occupied area, and is helpful to reduce the production cost; by arranging a first intensified mass transfer unit in the oxidation reactor, the gas phase raw material enters the oxidation reactor after being treated by the first intensified mass transfer unit, thereby the gas-liquid contact area of the gas phase raw material and the liquid phase raw material can be increased, the gas-liquid mass transfer efficiency can be improved, and thus the reaction efficiency can be improved; by arranging a heat exchange pipeline, the temperature of the material in the oxidation reactor can be controlled by the first heat exchanger, the reaction temperature fluctuation caused by the heat release of the oxidation reaction can be prevented, the stability of the reaction temperature can be maintained, and thus the conversion rate and the selectivity of the reaction can be improved, and the yield of the reaction product can be improved. In addition, the heat exchange pipeline can play a role of local stirring of the material in the oxidation reactor during the heat exchange process of the material, which is helpful to uniformly distribute the micro-bubbles output by the first intensified mass transfer unit in the oxidation reactor, and avoid the coalescence of the bubbles, thereby further improving the reaction efficiency and the product yield. In summary, this scheme is helpful to improve the reaction efficiency and the product yield of the ethylbenzene peroxidation reaction, the concentration of ethylbenzene peroxide hydrogen in the reaction product is relatively high, and the needs of the downstream production can be met. In the related art, the ethylbenzene peroxidation reaction is usually carried out in multiple (for example, two) non-catalytic, liquid-phase series oxidation reactors, and the concentration of EBHP in the reaction product obtained after passing through multiple oxidation reactors is usually only 8-10 wt%. On the one hand, this production system needs to use multiple oxidation reactors, resulting in a relatively large overall occupied space; on the other hand, the concentration of EBHP in the reaction product obtained by this production system is relatively low, the reaction efficiency is low, and due to the relatively low concentration of EBHP, it cannot be directly applied to the downstream (for example, ethylbenzene peroxide hydrogen epoxidation reaction), and usually needs to increase the concentration equipment for further concentration, which further increases the production cost. In addition, the inventors have found through research that the reaction of ethylbenzene oxidation to generate hydrogen peroxide has the characteristics of slow reaction rate, sensitivity to temperature, great influence on product concentration, moderate reaction heat effect, etc., and thus the reactor of this reaction should meet the requirements of large liquid holdup, high heat transfer efficiency, stable operation, easy control of reaction conditions, etc. However, the inventors have further found that the liquid phase backmixing in the reactor (for example, a bubble column reactor) that can meet the requirement of large liquid holdup will seriously affect the reaction selectivity and the control of the reaction, and when the height-diameter ratio of the reactor is large, the coalescence of bubbles will occur, the bubble dispersion effect will become poor, the gas-liquid contact area will be reduced, and the gas-liquid mass transfer efficiency will be affected. In view of the above research, the embodiments of the present application provide an ethylbenzene intensified oxidation reaction system, which only uses one oxidation reactor, can reduce the occupied area, and is helpful to reduce the production cost; by arranging a first intensified mass transfer unit in the oxidation reactor, the gas phase raw material enters the oxidation reactor after being treated by the first intensified mass transfer unit, thereby the gas-liquid contact area of the gas phase raw material and the liquid phase raw material can be increased, the gas-liquid mass transfer efficiency can be improved, and thus the reaction efficiency can be improved; by arranging a heat exchange pipeline, the temperature of the material in the oxidation reactor can be controlled by the first heat exchanger, the reaction temperature fluctuation caused by the heat release of the oxidation reaction can be prevented, the stability of the reaction temperature can be maintained, and thus the conversion rate and the selectivity of the reaction can be improved, and the yield of the reaction product can be improved. In addition, the heat exchange pipeline can play a role of local stirring of the material in the oxidation reactor during the heat exchange process of the material, which is helpful to uniformly distribute the micro-bubbles output by the first intensified mass transfer unit in the oxidation reactor, and avoid the coalescence of the bubbles, thereby further improving the reaction efficiency and the product yield. In summary, this scheme is helpful to improve the reaction efficiency and the product yield of the ethylbenzene peroxidation reaction, the concentration of ethylbenzene peroxide hydrogen in the reaction product is relatively high, and the needs of the downstream production can be met. Preferably, it also includes a circulation pipe; the inlet of the circulation pipe is connected to the bottom of the oxidation reactor; the outlet of the circulation pipe is connected to the oxidation reactor, the outlet of the circulation pipe is vertically higher than the inlet of the circulation pipe and vertically lower than the liquid level of the oxidation reactor; the liquid inlet pipe is connected to the circulation pipe, and the liquid phase feedstock in the liquid inlet pipe enters the oxidation reactor through the circulation pipe; a second enhanced mass transfer unit is installed near the outlet of the circulation pipe, the second enhanced mass transfer unit is connected to the gas inlet pipe, and the gas phase feedstock in the gas inlet pipe is processed by the second enhanced mass transfer unit before entering the circulation pipe to enhance the mass transfer effect between the gas phase feedstock and the liquid phase feedstock; the product outlet is vertically higher than the outlet of the circulation pipe, and the product outlet is vertically located at the bottom of the oxidation reactor. Below the liquid surface. In the preferred embodiment described above, the material at the bottom of the oxidation reactor can be extracted using a circulation pipe and transported back to the oxidation reactor through the circulation pipe outlet. This stirs the material within the oxidation reactor, promoting the uniform distribution of microbubbles and thus further improving reaction efficiency and product yield. Furthermore, by installing a second enhanced mass transfer unit within the circulation pipe, the conveying power of the gaseous raw material in the inlet pipe and the conveying power of the material in the circulation pipe can be used simultaneously to disperse and break up the gaseous raw material, improving the dispersion and breaking effect. The microbubbles output from the second enhanced mass transfer unit can flow back to the oxidation reactor along with the circulating material under the impact of the material in the circulation pipe. Under this impact, the microbubbles can be further dispersed and broken up, and they can be more evenly distributed in the circulating material, preventing bubble aggregation. This helps to further increase the gas-liquid contact area, thereby further improving reaction efficiency and reaction yield. Preferably, a baffle is provided inside the oxidation reactor, with the top of the baffle vertically higher than the liquid surface of the oxidation reactor, and the distance between the bottom of the baffle and the bottom of the inner cavity of the oxidation reactor is a preset distance; a circulation channel is formed between the baffle and the side wall of the oxidation reactor, and the outlet of the circulation pipe is connected to the circulation channel. In the preferred embodiment described above, by setting up baffles, the material circulating back in the circulation pipe can be prevented from impacting the material that has already reacted in the oxidation reactor, thereby preventing backmixing and ensuring the orderly progress of the reaction within the oxidation reactor. Furthermore, the circulating material can flow into the bottom of the oxidation reactor along the circulation channel, which helps to extend the reaction path of this portion of the material, thus contributing to improving the conversion rate of the reactants. Preferably, the distance between the second intensified mass transfer unit and the inner wall of the oxidation reactor is less than the distance between the baffle and the inner wall of the oxidation reactor, and the distance between the baffle and the inner wall of the oxidation reactor is less than the distance between the baffle and the first intensified mass transfer unit; preferably, the second intensified mass transfer unit is arranged at the outlet of the circulation pipeline; preferably, the side of the baffle close to the side wall of the oxidation reactor is sequentially provided with a plurality of protrusions from top to bottom. In the present solution, considering that due to the fast flow of the material in the circulation pipeline, part of the micro-bubbles in the second intensified mass transfer unit may not be broken into smaller ones before being sent into the circulation pipeline, resulting in poor consistency of the micro-bubble size of the micro-bubble flow (which can be simply referred to as the first micro-bubble flow) output by the second intensified mass transfer unit, which may cause bubble coalescence during the process of entering the circulation channel through the circulation pipeline, affecting the contact area between gas and liquid. And because part of the micro-bubbles output by the second intensified mass transfer unit has a size larger than that of the micro-bubbles output by the first intensified mass transfer unit, when these micro-bubbles enter the interior of the oxidation reactor (here mainly refers to the chamber inside the oxidation reactor except the circulation channel), it may cause the micro-bubble size in the oxidation reactor to be inconsistent, thereby leading to uneven gas distribution in the oxidation reactor, affecting the reaction efficiency. In addition, the rising speed of micro-bubbles of different sizes in the oxidation reactor is different, which may cause coalescence between micro-bubbles of different sizes, and further affect the reaction efficiency of ethylbenzene peroxidation. In the solution of the present embodiment, by specifically setting the relative positional relationship between the second intensified mass transfer unit, the baffle and the first intensified mass transfer unit, the first micro-bubble flow can quickly enter the circulation channel, and the micro-bubbles in the first micro-bubble flow can be further dispersed and broken when colliding with the baffle, avoiding bubble coalescence. At the same time, the micro-bubbles in the first micro-bubble flow gradually decrease during the process of entering the oxidation reactor along the circulation channel, and when the micro-bubble flow output by the second intensified mass transfer unit flows near the first intensified mass transfer unit, the size of the micro-bubbles in the first micro-bubble flow is nearly consistent with the size of the micro-bubbles output by the first intensified mass transfer unit, thereby avoiding the influence of the micro-bubble size on the reaction efficiency of ethylbenzene peroxidation. In a further preferred solution, the second intensified mass transfer unit is arranged at the outlet of the circulation pipeline. Thus, the first micro-bubble flow can be directly input into the circulation channel, avoiding bubble coalescence during the flow of the first micro-bubble flow in the circulation pipeline. In a further preferred solution, a plurality of protrusions are sequentially arranged on the baffle from top to bottom, so that the micro-bubbles output by the second intensified mass transfer unit can collide with these protrusions when flowing in the circulation channel, further breaking the micro-bubbles, which helps to further reduce the size difference between the micro-bubbles output by the second intensified mass transfer unit and the micro-bubbles output by the first intensified mass transfer unit. ​Preferably, a second heat exchanger is arranged on the circulation pipeline, and the material in the circulation pipeline is circulated to the oxidation reactor after being heated by the second heat exchanger; preferably, a circulation pump is arranged on the circulation pipeline, and the circulation pump is located in front of the second heat exchanger along the flow direction of the liquid in the circulation pipeline. The above scheme can control the temperature of the material in the oxidation reactor by arranging the second heat exchanger on the circulation pipeline, thereby maintaining the stability of the reaction temperature, and further improving the conversion rate and selectivity of the reaction, and improving the yield of the reaction product. Preferably, the number of the first enhanced mass transfer units is multiple, and the multiple first enhanced mass transfer units are arranged in the vertical direction below the product outlet; preferably, the multiple first enhanced mass transfer units are arranged in the vertical direction from top to bottom; preferably, the outlets of the multiple first enhanced mass transfer units are downward. In the above scheme, the dispersion and fragmentation efficiency of the gas-phase raw material can be improved by arranging multiple first enhanced mass transfer units; the uniformity of the micro-bubble distribution in the oxidation reactor can be improved by arranging the multiple first enhanced mass transfer units in the vertical direction from top to bottom, thereby further improving the gas-liquid contact area. In addition, in the above one of the preferred schemes, the outlets of the multiple first enhanced mass transfer units are downward. It can be understood that in this scheme, the flow direction of the reaction raw material is from bottom to top, and the final reaction product is discharged from the product outlet at the top, so the liquid-phase raw material concentration is higher at the lower part of the first enhanced mass transfer unit than at the upper part of the first enhanced mass transfer unit. By supplementing the micro-bubbles of the dispersed and fragmented gas-phase raw material to the lower part of the first enhanced mass transfer unit, the liquid-phase raw material and the gas-phase raw material at the lower part can be more fully reacted, thereby further improving the reaction efficiency and the product yield. Preferably, the product outlet is arranged at the lower part of the oxidation reactor, the liquid inlet pipeline is communicated with the upper part of the oxidation reactor, and the liquid inlet pipeline is lower than the liquid level of the oxidation reactor in the vertical direction; the number of the first enhanced mass transfer units is multiple, and the multiple first enhanced mass transfer units are arranged in the vertical direction between the liquid inlet pipeline and the product outlet. In the above scheme, the dispersion and fragmentation efficiency of the gas-phase raw material can be improved by arranging multiple first enhanced mass transfer units; the uniformity of the micro-bubble distribution in the oxidation reactor can be improved by arranging the multiple first enhanced mass transfer units in the vertical direction from top to bottom, thereby further improving the gas-liquid contact area. Preferably, the outlets of the multiple first enhanced mass transfer units face upwards. It can be understood that in this configuration, the flow direction of the reactants is from top to bottom, and the final reaction product is discharged from the product outlet at the bottom. Therefore, compared to the bottom of the first enhanced mass transfer unit, the concentration of the liquid-phase feedstock above the first enhanced mass transfer unit is higher. By supplementing the top of the first enhanced mass transfer unit with microbubbles after the gas-phase feedstock is dispersed and broken, it helps to make the liquid-phase feedstock and gas-phase feedstock react more fully, thereby further improving the reaction efficiency and product yield. Preferably, there are multiple heat exchange pipes arranged sequentially from top to bottom. This arrangement allows for more precise control of the reaction temperature within the oxidation reactor, thereby contributing to improved conversion rate and selectivity. Furthermore, the multiple heat exchange pipes can agitate different areas within the oxidation reactor, further enhancing the uniformity of microbubble distribution and thus contributing to increased reaction efficiency and product yield. Preferably, the oxidation reactor has multiple layers of grids arranged alternately from top to bottom, with the grids located below the liquid surface. This design, by arranging multiple layers of grids alternately from top to bottom within the oxidation reactor, can minimize backmixing of the liquid phase and allow the reaction to proceed in a more orderly manner. Those skilled in the art will understand that the enhanced mass transfer reactor used in this invention has been described in the inventors' prior patents, such as applications CN201610641119.6, CN201610641251.7, CN201710766435.0, CN106187660, CN105903425A, CN109437390A, CN205833127U, and CN207581700U. The prior patent CN201610641119.6 details the specific product of the micron-sized bubble generator (i.e., bubble breaker). The application document describes the structure and working principle of a micron-sized bubble generator as follows: "The micron-sized bubble generator includes a main body and a secondary breaking component. The main body has a cavity, and an inlet communicating with the cavity is provided on the main body. The first and second ends of the cavity are both open, and the cross-sectional area of ​​the cavity decreases from the middle of the cavity towards the first and second ends. The secondary breaking component is located at at least one of the first and second ends of the cavity, and a part of the secondary breaking component is located inside the cavity. An annular channel is formed between the secondary breaking component and the open through holes at both ends of the cavity. The micron-sized bubble generator also includes an air inlet pipe and a liquid inlet pipe." From the specific structure disclosed in the application document, its specific working principle can be understood as follows: the liquid enters the micron-sized bubble generator tangentially through the liquid inlet pipe, rotates at ultra-high speed and cuts the gas, breaking the gas bubbles into micron-sized microbubbles, thereby increasing the mass transfer area between the liquid phase and the gas phase. Moreover, the micron-sized bubble generator in this patent belongs to a pneumatic bubble breaker. In addition, the prior patent 201610641251.7 discloses that a primary bubble breaker has a circulating liquid inlet, a circulating gas inlet and a gas-liquid mixture outlet, and a secondary bubble breaker is connected with the feeding inlet and the gas-liquid mixture outlet, which indicates that the bubble breaker needs gas-liquid mixture to enter, and from the subsequent drawings, it can be known that the primary bubble breaker mainly uses circulating liquid as power, so the primary bubble breaker actually belongs to a liquid-driven type of enhanced reactor, and the secondary bubble breaker is used for simultaneously feeding the gas-liquid mixture into an elliptical rotating ball to rotate, so that the bubble breaking is realized in the rotating process, and the secondary bubble breaker actually belongs to a gas-liquid linkage type of bubble breaker. Actually, whether the bubble breaker is a liquid-driven type or a gas-liquid linkage type, it belongs to a specific form of bubble breaker, and the enhanced mass transfer reactor adopted in the present application is not limited to the above-mentioned forms, and the specific structure of the bubble breaker disclosed in the prior patent is only one of the forms that can be adopted in the present application. In addition, the prior patent 201710766435.0 discloses that the principle of the bubble breaker is high-speed jet flow to achieve mutual collision of gas phases, and the prior patent CN106187660 also discloses the specific structure of the bubble breaker, and the specific structure is shown in the description in paragraphs

[0031] -

[0041] and The drawings part has a detailed description of the specific working principle of the bubble breaker S-2, the top of the bubble breaker is a liquid phase inlet, the side is a gas phase inlet, the liquid phase entering from the top provides a suction power, so that the effect of being broken into superfine bubbles is achieved, and it can be seen from the drawings that the bubble breaker has a conical structure, the diameter of the upper part is larger than that of the lower part, and this is also for the liquid phase to better provide the suction power. In the early stage of the prior patent application, the bubble breaker has just been developed, so it is named as a micron bubble generator (CN201610641119.6) in the early stage, and with continuous technical improvement, it is renamed as a bubble breaker in the later stage, and the enhanced mass transfer reactor in the present application is equivalent to the previous micron bubble generator, micro-interface generator and the like, only the name is different. In summary, the enhanced mass transfer reactor of the present application belongs to the prior art. The present application also provides an ethylbenzene enhanced oxidation reaction method, which adopts the system described above, and the method comprises the following steps: after the gas phase raw material is broken into micron-sized micro-bubbles by the enhanced mass transfer, the gas phase raw material is mixed with the liquid phase raw material to perform an oxidation reaction; wherein the gas phase raw material is air or oxygen, and the liquid phase raw material is ethylbenzene. Compared with the prior art, the present application has the following advantages: 1. The present application only uses one oxidation reactor, which can reduce the occupied area and help reduce the production cost. 2、The present application can improve the gas-liquid contact area of the gas phase raw material and the liquid phase raw material, improve the gas-liquid mass transfer efficiency, and thus improve the reaction efficiency by arranging the first mass transfer intensifier unit in the oxidation reactor. 3、The present application can control the temperature of the material in the oxidation reactor by the first heat exchanger, prevent the reaction temperature from fluctuating sharply due to the heat release of the oxidation reaction, maintain the stability of the reaction temperature, and thus help to improve the conversion rate and selectivity of the reaction and improve the yield of the reaction product. 4、In the present application, the heat exchange pipeline can play a local stirring role on the material in the oxidation reactor during the heat exchange process, which helps to make the micro-bubbles output by the first mass transfer intensifier unit uniformly distributed in the oxidation reactor, avoids the coalescence of the bubbles, and thus helps to further improve the reaction efficiency and the product yield. 4、In the present application, the heat exchange pipeline can play a local stirring role on the material in the oxidation reactor during the heat exchange process, which helps to make the micro-bubbles output by the first mass transfer intensifier unit uniformly distributed in the oxidation reactor, avoids the coalescence of the bubbles, and thus helps to further improve the reaction efficiency and the product yield. BRIEF DESCRIPTION OF DRAWINGS Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The detailed description is made with reference to the accompanying drawings. FIG. 1 shows a schematic diagram of an ethylbenzene intensified oxidation reaction system according to one embodiment of the present application; FIG. 2 shows a schematic diagram of an ethylbenzene intensified oxidation reaction system according to another embodiment of the present application. 1, oxidation reactor; 101, product outlet; 102, tail gas outlet; 2, baffle; 3, first mass transfer intensifier unit; 4, gas inlet pipeline; 5, heat exchange pump; 6, heat exchange pipeline; 7, first heat exchanger; 8, circulation pipeline; 9, second heat exchanger; 10, circulation pump; 11, liquid inlet pipeline; 12, baffle; 13, second mass transfer intensifier unit; 14, protrusion. DETAILED DESCRIPTION The technical solutions of the present application will be described clearly and completely below in combination with the drawings and specific embodiments, but those skilled in the art will understand that the following described embodiments are part of the embodiments of the present application, not all the embodiments, and are only used to illustrate the present application, and should not be considered as limiting the scope of the present application. Based on the embodiments in the present application, all other embodiments obtained by those skilled in the art without making creative efforts are within the scope of protection of the present application. The specific conditions are not specified in the embodiments, and are carried out according to the conventional conditions or the conditions recommended by the manufacturer. The reagents or instruments used are not specified by the manufacturer, and are conventional products that can be purchased on the market. In the description of the present application, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer" and the like indicate the orientation or positional relationship shown in the drawings based on the orientation or positional relationship, and are only for the purpose of facilitating the description of the present application and simplifying the description, and do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as a limitation of the present application. In addition, the terms "first", "second", "third" are only for the purpose of description, and cannot be understood as indicating or implying relative importance. In the description of the present application, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer" and the like indicate the orientation or positional relationship shown in the drawings based on the orientation or positional relationship, and are only for the purpose of facilitating the description of the present application and simplifying the description, and do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as a limitation of the present application. In addition, the terms "first", "second", "third" are only for the purpose of description, and cannot be understood as indicating or implying relative importance. In the description of the present application, it should be noted that the terms "installation", "connection", "connection" should be understood in a broad sense unless otherwise specified and limited, for example, it can be fixed connection, or detachable connection, or integral connection; it can be mechanical connection, or electrical connection; it can be directly connected, or indirectly connected through an intermediate medium, or it can be the communication inside two elements. For those skilled in the art, the specific meaning of the above terms in the present application can be understood according to the specific circumstances. In order to more clearly describe the technical solutions in the present application, the following will be described in the form of specific examples. Example 1 Figure 1 shows a schematic diagram of an ethylbenzene intensified oxidation reaction system according to an embodiment of the present application. As shown in Figure 1, the ethylbenzene intensified oxidation reaction system comprises: an oxidation reactor 1, the oxidation reactor 1 is connected with a gas inlet pipeline 4 for inputting gas phase raw material and a liquid inlet pipeline 11 for inputting liquid phase raw material; the side wall of the oxidation reactor 1 is provided with a product outlet 101; a first intensified mass transfer unit 3, the first intensified mass transfer unit 3 is arranged inside the oxidation reactor 1, the gas inlet pipeline 4 is connected with the first intensified mass transfer unit 3, the gas phase raw material in the gas inlet pipeline 4 is treated by the first intensified mass transfer unit 3 and then enters the oxidation reactor 1, so as to enhance the mass transfer effect between the gas phase raw material and the liquid phase raw material; a heat exchange pipeline 6, the inlet and outlet of the heat exchange pipeline 6 are communicated with the oxidation reactor 1, and the inlet of the heat exchange pipeline 6 is arranged below the outlet of the heat exchange pipeline 6 in the vertical direction; a first heat exchanger 7 is arranged on the heat exchange pipeline 6. In the embodiment of the present application, the liquid phase raw material is ethylbenzene, and the gas phase raw material can be air or oxygen. The reactor can be a bubble column reactor. In the embodiment of the present application, the first mass transfer intensifier unit 3 is arranged inside the oxidation reactor 1. Optionally, the mass transfer intensifier unit can be composed of one or more mass transfer intensifier reactors. During the operation of the oxidation reactor 1, the gas-phase raw material can be dispersed into micron-sized micro-bubbles by the first mass transfer intensifier unit, so as to increase the phase interface mass transfer area between the gas-phase raw material and the liquid-phase raw material, thereby enhancing the mass transfer effect between the gas-phase raw material and the liquid-phase raw material. In the embodiment shown in Fig. 1, the first mass transfer intensifier unit 3 comprises one mass transfer intensifier reactor. Optionally, the heat exchange pump 5 can be arranged on the heat exchange pipeline 6. In the embodiment shown in Fig. 1, the heat exchange pump 5 can be arranged in front of the first heat exchanger along the material flow direction inside the heat exchange pipeline 6, thereby reducing the operation resistance of the heat exchange pump 5. Preferably, as shown in Fig. 1, the ethylbenzene intensified oxidation reaction system further comprises a circulation pipeline 8; the inlet of the circulation pipeline 8 is in communication with the bottom of the oxidation reactor 1; the outlet of the circulation pipeline 8 is in communication with the oxidation reactor 1, the outlet of the circulation pipeline 8 is higher than the inlet of the circulation pipeline 8 in the vertical direction, and the outlet of the circulation pipeline 8 is lower than the liquid level of the oxidation reactor 1 in the vertical direction; a liquid inlet pipeline 11 is in communication with the circulation pipeline 8, the liquid-phase raw material in the liquid inlet pipeline 11 enters the oxidation reactor 1 through the circulation pipeline 8; a second mass transfer intensifier unit 13 is arranged near the outlet of the circulation pipeline 8 inside the circulation pipeline 8, the second mass transfer intensifier unit 13 is connected with the gas inlet pipeline 4, the gas-phase raw material in the gas inlet pipeline 4 enters the circulation pipeline 8 after being treated by the second mass transfer intensifier unit 13, so as to enhance the mass transfer effect between the gas-phase raw material and the liquid-phase raw material; the product outlet 101 is higher than the outlet of the circulation pipeline 8 in the vertical direction, and the product outlet 101 is below the liquid level of the oxidation reactor 1 in the vertical direction. In the embodiment shown in Fig. 1, the second mass transfer intensifier unit 13 comprises one mass transfer intensifier reactor. It can be understood that the gas inlet pipeline 4 connected with the first mass transfer intensifier unit 3 and the gas inlet pipeline 4 connected with the second mass transfer intensifier unit 13 can be the same gas inlet pipeline, in which case, the gas inlet pipeline 4 can be provided with multiple branch pipelines to be connected with different mass transfer intensifier units. Of course, The gas inlet pipeline 4 connected with the first mass transfer intensifier unit 3 and the gas inlet pipeline 4 connected with the second mass transfer intensifier unit 13 can also be independent gas inlet pipelines, which will not be described herein. Preferably, as shown in Fig. 1, the oxidation reactor 1 is provided with a baffle 12, the top of the baffle 12 is higher than the liquid level of the oxidation reactor 1 in the vertical direction, and the distance between the bottom of the baffle 12 and the bottom of the inner cavity of the oxidation reactor 1 is a preset distance; the baffle 12 and the side wall of the oxidation reactor 1 form a circulation channel, and the outlet of the circulation pipeline 8 is in communication with the circulation channel. The preset distance can be set according to actual needs, so as to facilitate the outflow of the material in the circulation channel through the bottom of the baffle 12 and the bottom of the inner cavity of the oxidation reactor 1. Preferably, as shown in Fig. 1, the distance between the second enhanced mass transfer unit 13 and the inner wall of the oxidation reactor 1 is smaller than the distance between the baffle 12 and the inner wall of the oxidation reactor 1, and the distance between the baffle 12 and the first enhanced mass transfer unit 3. Preferably, as shown in Fig. 1, the second enhanced mass transfer unit 13 is arranged at the outlet of the circulation pipeline. Preferably, as shown in Fig. 1, the baffle 12 is provided with a plurality of protrusions 14 arranged from top to bottom on one side close to the side wall of the oxidation reactor 1. Preferably, as shown in Fig. 1, the circulation pipeline 8 is provided with a second heat exchanger 9, and the material in the circulation pipeline 8 is circulated into the oxidation reactor 1 after heat exchange through the second heat exchanger 9. Preferably, as shown in Fig. 1, the circulation pipeline 8 is provided with a circulation pump 10, and the circulation pump 10 is located in front of the second heat exchanger 9 along the flow direction of the liquid in the circulation pipeline 8. Preferably, as shown in Fig. 1, the number of the first enhanced mass transfer units 3 is multiple, and the multiple first enhanced mass transfer units 3 are all lower than the product outlet 101 in the vertical direction. Preferably, as shown in Fig. 1, the multiple first enhanced mass transfer units 3 are arranged from top to bottom in the vertical direction. Preferably, as shown in Fig. 1, the outlets of the multiple first enhanced mass transfer units 3 are downward. Preferably, as shown in Fig. 1, the number of the heat exchange pipelines 6 is multiple, and the multiple heat exchange pipelines 6 are arranged from top to bottom. The number of the heat exchange pipelines 6 can be selected according to the height of the oxidation reactor 1, which is not described herein. In the embodiment shown in Fig. 1, the number of the heat exchange pipelines 6 is two. Preferably, as shown in Fig. 1, the multiple layers of the grates 2 are arranged from top to bottom in the oxidation reactor 1, and the multiple layers of the grates 2 are located below the liquid surface of the oxidation reactor 1. The embodiment also provides an ethylbenzene enhanced oxidation reaction method, which adopts the ethylbenzene enhanced oxidation reaction system described above, and the method comprises: mixing the gas-phase raw material and the liquid-phase raw material after the gas-phase raw material is broken into micron-sized micro-bubbles by the enhanced mass transfer, and then performing oxidation reaction; wherein the gas-phase raw material is air or oxygen, and the liquid-phase raw material is ethylbenzene. The reaction product can be extracted from the product outlet 101, and the tail gas in the reaction process is discharged through the tail gas outlet 102. Embodiment 2 The difference between the embodiment and the embodiment 1 is that the embodiment does not arrange the circulation pipeline 8, and the second enhanced mass transfer unit 13 is arranged in the circulation channel, and the liquid inlet pipeline 11 directly communicates with the circulation channel. Embodiment 3 The difference between the embodiment and the embodiment 1 is that the embodiment does not arrange the second enhanced mass transfer unit 13. Embodiment 4 The difference between this embodiment and embodiment 1 is that this embodiment does not provide the baffle 12. Embodiment 5 The difference between this embodiment and embodiment 1 is that this embodiment does not provide the second heat exchanger 9. Embodiment 6 The difference between this embodiment and embodiment 1 is that in this embodiment, the multiple first enhanced mass transfer units 3 are arranged in sequence along the horizontal direction. Embodiment 7 The difference between this embodiment and embodiment 1 is that in this embodiment, the baffle 2 is not provided. Embodiment 8 The difference between this embodiment and embodiment 1 is that in this embodiment, the multiple heat exchange pipes 6 are arranged in sequence along the horizontal direction. Embodiment 9 The difference between this embodiment and embodiment 1 is that in this embodiment, the distance between the baffle and the inner wall of the oxidation reactor is greater than the distance between the baffle and the first enhanced mass transfer unit. Embodiment 10 The difference between this embodiment and embodiment 1 is that in this embodiment, the distance between the baffle and the inner wall of the oxidation reactor is greater than the distance between the second enhanced mass transfer unit and the inner wall of the oxidation reactor. Embodiment 11 Figure 2 shows a schematic diagram of an ethylbenzene enhanced oxidation reaction system according to another embodiment of the present application. As shown in Figure 2, the ethylbenzene enhanced oxidation reaction system comprises an oxidation reactor 1, the oxidation reactor 1 being connected with a gas inlet pipe 4 for inputting a gas phase raw material and a liquid inlet pipe 11 for inputting a liquid phase raw material; the oxidation reactor 1 is provided with a product outlet 101 on the side wall; a first enhanced mass transfer unit 3 is arranged inside the oxidation reactor 1, the gas inlet pipe 4 is connected with the first enhanced mass transfer unit 3, and the gas phase raw material in the gas inlet pipe 4 is treated by the first enhanced mass transfer unit 3 before entering the oxidation reactor 1, so as to enhance the mass transfer effect between the gas phase raw material and the liquid phase raw material; a heat exchange pipe 6 is arranged in the oxidation reactor 1, the inlet and outlet of the heat exchange pipe 6 are communicated with the oxidation reactor 1, and the inlet of the heat exchange pipe 6 is arranged below the outlet of the heat exchange pipe 6 along the vertical direction; and a first heat exchanger 7 is arranged on the heat exchange pipe 6. In the embodiments of the present application, the liquid phase raw material is ethylbenzene, and the gas phase raw material can be air or oxygen. The reactor can be a bubble column reactor. In the embodiments of the present application, the oxidation reactor 1 is provided with the first enhanced mass transfer unit 3 inside. Optionally, the enhanced mass transfer unit can be composed of one or more enhanced mass transfer reactors. When the reactor is working, the gas phase raw material can be dispersed and broken into micron-level micro-bubbles by the enhanced mass transfer unit, The first enhanced mass transfer unit 3 is arranged to increase the phase boundary mass transfer area between the gas phase raw material and the liquid phase raw material, thereby enhancing the mass transfer effect between the gas phase raw material and the liquid phase raw material. Optionally, a heat exchange pump 5 can be arranged on the heat exchange pipeline 6. In the embodiment shown in Fig. 2, the heat exchange pump 5 can be arranged in front of the first heat exchanger along the material flow direction in the heat exchange pipeline 6, thereby reducing the operating resistance of the heat exchange pump 5. Preferably, as shown in Fig. 2, the product outlet 101 is arranged at the lower part of the oxidation reactor 1, the liquid inlet pipeline 11 is in communication with the upper part of the oxidation reactor 1, and the liquid inlet pipeline 11 is vertically lower than the liquid level of the oxidation reactor 1; the number of the first enhanced mass transfer units 3 is multiple, and the multiple first enhanced mass transfer units 3 are sequentially arranged in the vertical direction between the liquid inlet pipeline 11 and the product outlet 101. Preferably, as shown in Fig. 2, the outlets of the multiple first enhanced mass transfer units 3 are upward. Preferably, as shown in Fig. 2, the number of the heat exchange pipelines 6 is multiple, and the multiple heat exchange pipelines 6 are sequentially arranged from top to bottom. In the embodiment shown in Fig. 2, the number of the heat exchange pipelines 6 is two. Preferably, as shown in Fig. 2, multiple layers of the baffle plates 2 are arranged in the oxidation reactor 1 from top to bottom, and the multiple layers of the baffle plates 2 are below the liquid level of the oxidation reactor 1. The embodiment also provides an ethylbenzene enhanced oxidation reaction method, which uses the above-mentioned ethylbenzene enhanced oxidation reaction system. The method comprises: mixing the gas phase raw material and the liquid phase raw material after the gas phase raw material is broken into micron-sized micro-bubbles by the first enhanced mass transfer unit 3 to perform an oxidation reaction; wherein the gas phase raw material is air or oxygen, and the liquid phase raw material is ethylbenzene. The reaction product can be extracted from the product outlet 101, and the tail gas in the reaction process is discharged through the tail gas outlet 102. Example 12 The difference between the embodiment and the embodiment 11 is that the multiple first enhanced mass transfer units 3 are sequentially arranged in the horizontal direction in the embodiment. Example 13 The difference between the embodiment and the embodiment 11 is that the baffle plate 2 is not arranged in the embodiment. Example 14 The difference between the embodiment and the embodiment 11 is that the multiple heat exchange pipelines 6 are sequentially arranged in the horizontal direction in the embodiment. Comparative Example 1 The difference between the embodiment and the embodiment 1 is that the first enhanced mass transfer unit 3 is not arranged. Comparative Example 2 The difference between the embodiment and the embodiment 1 is that the first heat exchanger 7 is not arranged. Comparative Example 3 The only difference between this embodiment and Embodiment 1 is that the heat exchange pipe 6 is not provided. Comparative Example 4 The only difference between this embodiment and embodiment 11 is that the first enhanced mass transfer unit 3 is not provided. Comparative Example 5 The only difference between this embodiment and embodiment 11 is that the first heat exchanger 7 is not provided. Comparative Example 6 The only difference between this embodiment and embodiment 11 is that the heat exchange pipe 6 is not provided. Comparative Example 7 In this embodiment, two non-catalytic, liquid-phase series oxidation reactors are used as reactors for the ethylbenzene peroxidation reaction. Experimental Example Ethylbenzene hydrogen peroxide was prepared using ethylbenzene-enhanced oxidation systems as described in Examples 1-14 and Comparative Examples 1-7. The gaseous feedstock was air, the liquid feedstock was ethylbenzene, and the reaction temperature in the oxidation reactor was 145°C, with a pressure of 0.24 MPa. The ethylbenzene content in the product of each ethylbenzene-enhanced oxidation system was measured. The concentration of hydrogen peroxide and the test results are shown in Table 1. Table 1 Concentration of ethylbenzene hydrogen peroxide in the products The concentration of ethylbenzene hydrogen peroxide in the product obtained in Example 1 is compared with that in Example 2. The concentration of ethylbenzene hydrogen peroxide in the product of Example 1 is significantly higher than that of Example 2. This is because Example 1, by setting up a circulation pipe, can stir the material in the oxidation reactor, improving the uniformity of microbubble distribution within the reactor. Furthermore, the microbubbles output from the second enhanced mass transfer unit can flow back into the oxidation reactor along with the circulating material under the impact of the material in the circulation pipe. Under this impact, the microbubbles can be further dispersed and broken, and they can be more evenly distributed in the circulating material, avoiding bubble aggregation. This helps to further increase the gas-liquid contact area, thereby further improving reaction efficiency and yield. In summary, the scheme of Example 1, by combining the circulation pipe with the second enhanced mass transfer unit, helps to increase the concentration of ethylbenzene hydrogen peroxide in the product. Comparing the concentration of ethylbenzene hydrogen peroxide in the product obtained in Example 1 with that in the product obtained in Example 3, it can be seen that the concentration of ethylbenzene hydrogen peroxide in the product of Example 1 is higher than that in Example 3. This may be because a second enhanced mass transfer unit was installed in the circulation pipeline in the scheme of Example 1, which enhanced the dispersion and crushing effect of the gaseous raw material, thereby further increasing the concentration of ethylbenzene hydrogen peroxide in the product. Comparing the concentration of ethylbenzene hydrogen peroxide in the product obtained in Example 1 with that in the product obtained in Example 4, it can be seen that the concentration of ethylbenzene hydrogen peroxide in the product of Example 1 is higher than that in Example 4. This may be because the material circulating back into the oxidation reactor in the circulation pipeline in Example 4 impacted the reaction products in the oxidation reactor, causing backmixing of the reaction products and inhibiting the occurrence of the ethylbenzene peroxidation reaction. Therefore, the concentration of ethylbenzene hydrogen peroxide in the reaction products of that ethylbenzene peroxidation reaction is lower. Comparing the concentration of ethylbenzene hydrogen peroxide in the product obtained in Example 1 with that in the product obtained in Example 5, it can be seen that the concentration of ethylbenzene hydrogen peroxide in the product of Example 1 is higher than that in Example 5. This may be because a second exchanger was installed on the circulation pipeline of Example 1. The heater allows for better control of the reaction temperature, resulting in a more stable reaction temperature within the oxidation reactor, thus leading to a higher concentration of ethylbenzene hydrogen peroxide in the obtained product. Comparing the concentration of ethylbenzene hydrogen peroxide in the product obtained in Example 1 with that in the product obtained in Example 6, it can be seen that the concentration of ethylbenzene hydrogen peroxide in the product of Example 1 is higher than that in Example 6. This may be because the microbubbles output from the multiple horizontally arranged first enhanced mass transfer units are all at the same height in the oxidation reactor, causing bubble aggregation, which affects the reaction efficiency and yield. As a result, the concentration of ethylbenzene hydrogen peroxide in the reaction product of the ethylbenzene peroxidation reaction in Example 6 is lower. Comparing the concentration of ethylbenzene hydrogen peroxide in the product obtained in Example 1 with that in the product obtained in Example 7, it can be seen that the concentration of ethylbenzene hydrogen peroxide in the product of Example 1 is higher than that in Example 7. This may be because in Example 1, by setting up a barrier, liquid phase backmixing was further avoided, thereby ensuring the orderly progress of the ethylbenzene peroxidation reaction, resulting in a higher concentration of ethylbenzene hydrogen peroxide in the obtained product. Comparing the concentration of ethylbenzene hydrogen peroxide in the product obtained in Example 1 with that in the product obtained in Example 8, it can be seen that the concentration of ethylbenzene hydrogen peroxide in the product of Example 1 is higher than that in Example 8. This may be because in Example 1, multiple heat exchange pipes are set at different heights, resulting in better temperature control within the oxidation reactor, thus leading to a higher concentration of ethylbenzene hydrogen peroxide in the obtained product. Comparing the concentration of ethylbenzene hydrogen peroxide in the product obtained in Example 1 and the product obtained in Example 9, it can be seen that the concentration of ethylbenzene hydrogen peroxide in the product of Example 1 is higher than that in Example 9. This may be because in Example 9, the distance between the baffle and the inner wall of the oxidation reactor is greater than the distance between the baffle and the first enhanced mass transfer unit. At this time, the width of the circulation channel is larger, and the internal material flow rate is relatively slower. At this time, the microbubbles with inconsistent sizes in the first microbubble flow may have undergone bubble coalescence inside, generating larger microbubbles. These microbubbles flow to When the microbubble flow is near the first enhanced mass transfer unit, the distribution of microbubbles in the vicinity becomes uneven, affecting the reaction efficiency. Simultaneously, because the distance between the baffle and the first enhanced mass transfer unit is relatively short, the uneven-sized microbubble flow from the circulation channel, containing larger microbubbles, flows directly to the vicinity of the first enhanced mass transfer unit. This may cause direct collisions with the microbubble flow output from the first enhanced mass transfer unit, resulting in the formation of even larger microbubbles, further exacerbating the uneven distribution of microbubbles near the first enhanced mass transfer unit. For these reasons, the concentration of ethylbenzene hydrogen peroxide in the reaction products of the oxidation reactor in Example 9 is lower than that in Example 1. Comparing the concentration of ethylbenzene hydrogen peroxide in the product obtained in Example 1 with that in the product obtained in Example 10, it can be seen that the concentration of ethylbenzene hydrogen peroxide in the product of Example 1 is higher than that in Example 10. This may be because the distance between the baffle and the inner wall of the oxidation reactor in Example 10 is greater than the distance between the second enhanced mass transfer unit and the inner wall of the oxidation reactor. In this case, bubble coalescence may have occurred during the flow of the first microbubble stream in the circulation pipe, generating larger microbubbles. This increases the size difference between the microbubbles in the first microbubble stream and the microbubbles output from the first enhanced mass transfer unit, resulting in uneven distribution of microbubbles near the first enhanced mass transfer unit and affecting the reaction efficiency. Consequently, the concentration of ethylbenzene hydrogen peroxide in the reaction product in the oxidation reactor of Example 10 is lower than that in Example 1. Based on the data from Examples 1, 9, and 10, it can be seen that the solution in Example 1 of the present invention effectively improves the reaction efficiency of the ethylbenzene peroxidation reaction by specifically setting the relative positional relationship between the first enhanced mass transfer unit, the baffle, and the second enhanced mass transfer unit. Comparing the concentration of ethylbenzene hydrogen peroxide in the product obtained in Example 1 with that in Comparative Example 1, it can be seen that the concentration of ethylbenzene hydrogen peroxide in the product of Example 1 is significantly higher than that in Comparative Example 1. This may be because Example 1, by setting up multiple first enhanced mass transfer units, can increase the gas-liquid contact area, and the gas inlet pipe can supply gaseous feedstock to different height sections of the oxidation reactor through multiple first enhanced mass transfer units, ensuring that the gaseous feedstock is always in excess. Thus, the reaction yield and the raw material conversion rate are improved. Comparing the concentration of ethylbenzene hydroperoxide in the product obtained in Comparative Example 1 with the concentration of ethylbenzene hydroperoxide in the product obtained in Comparative Example 2, it can be seen that the concentration of ethylbenzene hydroperoxide in the product of Example 1 is obviously higher than that of Comparative Example 2. This can be due to the fact that in Example 1, by arranging the first heat exchanger, the temperature in the oxidation reactor can be more accurately controlled, so that the temperature in the oxidation reactor is more stable, and thus the concentration of ethylbenzene hydroperoxide in the obtained product is higher. Comparing the concentration of ethylbenzene hydroperoxide in the product obtained in Comparative Example 1 with the concentration of ethylbenzene hydroperoxide in the product obtained in Comparative Example 3, it can be seen that the concentration of ethylbenzene hydroperoxide in the product of Example 1 is obviously higher than that of Comparative Example 3. This can be due to the fact that in Example 1, by arranging the heat exchange pipe, on the one hand, the material can be stirred to improve the uniformity of the distribution of micro-bubbles in the oxidation reactor, and on the other hand, the heat exchange pipe can maintain the reaction temperature in the oxidation reactor through the first heat exchanger to make the reaction more orderly. Therefore, the concentration of ethylbenzene hydroperoxide in the obtained product is higher. Comparing the concentration of ethylbenzene hydroperoxide in the product obtained in Comparative Example 11 with the concentration of ethylbenzene hydroperoxide in the product obtained in Example 12, it can be seen that the concentration of ethylbenzene hydroperoxide in the product of Example 11 is obviously higher than that of Example 12. This can be due to the fact that the micro-bubbles output by the horizontally arranged multiple first enhanced mass transfer units are all at the same height section of the oxidation reactor, causing bubble coalescence, which affects the reaction efficiency and yield. Comparing the concentration of ethylbenzene hydroperoxide in the product obtained in Comparative Example 11 with the concentration of ethylbenzene hydroperoxide in the product obtained in Example 13, it can be seen that the concentration of ethylbenzene hydroperoxide in the product of Example 11 is obviously higher than that of Example 13. This can be due to the fact that in Example 11, by arranging the grating, liquid phase backmixing is further avoided, thereby ensuring the orderly progress of the ethylbenzene peroxidation reaction, and thus the concentration of ethylbenzene hydroperoxide in the obtained product is higher. Comparing the concentration of ethylbenzene hydroperoxide in the product obtained in Comparative Example 11 with the concentration of ethylbenzene hydroperoxide in the product obtained in Example 14, it can be seen that the concentration of ethylbenzene hydroperoxide in the product of Example 11 is obviously higher than that of Example 14. This can be due to the fact that in Example 11, multiple heat exchange pipes are arranged at different height positions, which can better control the temperature in the oxidation reactor, and thus the concentration of ethylbenzene hydroperoxide in the obtained product is higher. Comparing the concentration of ethylbenzene hydroperoxide in the product obtained in Comparative Example 11 with the concentration of ethylbenzene hydroperoxide in the product obtained in Example 14, it can be seen that the concentration of ethylbenzene hydroperoxide in the product of Example 11 is obviously higher than that of Example 14. This can be due to the fact that in Example 11, multiple heat exchange pipes are arranged at different height positions, which can better control the temperature in the oxidation reactor, and thus the concentration of ethylbenzene hydroperoxide in the obtained product is higher. Compared with the concentration of ethylbenzene hydroperoxide in the product obtained in Comparative Example 11 and the concentration of ethylbenzene hydroperoxide in the product obtained in Comparative Example 4, it can be seen that the concentration of ethylbenzene hydroperoxide in the product of Example 11 is significantly higher than that of Comparative Example 4, and the concentration of ethylbenzene hydroperoxide in the product of Example 11 is close to 2.7 times the concentration of Comparative Example 4. This may be because Example 11 can increase the gas-liquid contact area by arranging multiple first enhanced mass transfer units, and the gas inlet pipeline can supplement the gas phase raw material to different height sections of the oxidation reactor through multiple first enhanced mass transfer units, so as to ensure that the gas phase raw material is always in excess, thereby improving the reaction yield and raw material conversion rate. Compared with the concentration of ethylbenzene hydroperoxide in the product obtained in Comparative Example 11 and the concentration of ethylbenzene hydroperoxide in the product obtained in Comparative Example 5, it can be seen that the concentration of ethylbenzene hydroperoxide in the product of Example 11 is significantly higher than that of Comparative Example 5, and the concentration of ethylbenzene hydroperoxide in the product of Example 11 is close to 1.7 times the concentration of Comparative Example 5. This may be due to the fact that in Example 11, by arranging the first heat exchanger, the temperature in the oxidation reactor can be more accurately controlled, so that the temperature in the oxidation reactor is more stable, and therefore the concentration of ethylbenzene hydroperoxide in the obtained product is higher. Compared with the concentration of ethylbenzene hydroperoxide in the product obtained in Comparative Example 11 and the concentration of ethylbenzene hydroperoxide in the product obtained in Comparative Example 6, it can be seen that the concentration of ethylbenzene hydroperoxide in the product of Example 11 is significantly higher than that of Comparative Example 6, and the concentration of ethylbenzene hydroperoxide in the product of Comparative Example 6 is only half of that of Example 11. This may be due to the fact that in Example 11, by arranging the heat exchange pipeline, on the one hand, the material can be stirred to improve the uniformity of the distribution of micro-bubbles in the oxidation reactor, and on the other hand, the heat exchange pipeline can maintain the reaction temperature in the oxidation reactor through the first heat exchanger to make the reaction more orderly. Therefore, the concentration of ethylbenzene hydroperoxide in the obtained product is significantly higher than that of Comparative Example 6. Comparative Example 7 is a scheme adopted in the related art. Compared with Comparative Examples 1-14 and Comparative Example 7, it can be seen that the concentration of ethylbenzene hydroperoxide in the reaction product in Examples 1-14 is significantly higher than that of Comparative Example 7. This shows that the ethylbenzene enhanced oxidation reaction system of the present application can significantly improve the reaction efficiency and product yield of the ethylbenzene hydroperoxidation reaction, and the concentration of ethylbenzene hydroperoxide in Examples 1-14 basically meets the requirements of the downstream epoxidation reaction (i.e. the concentration of ethylbenzene hydroperoxide in the product is about 40 wt%). Therefore, when the system of the present application is applied to the PO / SM co-production process, there is no need to set a concentration unit for further concentration of the product, and the reaction product of the reactor can be directly sent to the epoxidation reactor, which can reduce the occupied area of the production system adopted in the PO / SM co-production process and reduce the production cost. It should be noted that the above embodiments are only used to illustrate the technical solutions of the present application, and are not intended to limit the present application; although the present application has been described in detail with reference to the above embodiments, those skilled in the art should understand that the technical solutions recorded in the above embodiments can be modified, or some or all of the technical features can be replaced by equivalents; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the scope of the technical solutions of the embodiments of the present application.

Claims

1. An ethylbenzene potentiated oxidation reaction system, characterized by, The application relates to an oxidation reactor, which comprises: an oxidation reactor connected with a gas inlet pipeline for inputting gas-phase raw materials and a liquid inlet pipeline for inputting liquid-phase raw materials; a product outlet is arranged on the side wall of the oxidation reactor; a first mass transfer intensifier arranged in the oxidation reactor, the gas inlet pipeline is connected with the first mass transfer intensifier, and the gas-phase raw materials in the gas inlet pipeline are treated by the first mass transfer intensifier and then enter the oxidation reactor, so that the mass transfer effect between the gas-phase raw materials and the liquid-phase raw materials is enhanced; a heat exchange pipeline, the inlet and outlet of the heat exchange pipeline are communicated with the oxidation reactor, the inlet of the heat exchange pipeline is arranged below the outlet of the heat exchange pipeline in the vertical direction, and a first heat exchanger is arranged on the heat exchange pipeline.

2. The ethylbenzene potentiated oxidation reaction system according to claim 1, characterized in that, a circulation pipeline, the inlet of the circulation pipeline is communicated with the bottom of the oxidation reactor, the outlet of the circulation pipeline is communicated with the oxidation reactor, the outlet of the circulation pipeline is higher than the inlet of the circulation pipeline in the vertical direction and is lower than the liquid surface of the oxidation reactor in the vertical direction; the liquid inlet pipeline is communicated with the circulation pipeline, and the liquid-phase raw materials in the liquid inlet pipeline enter the oxidation reactor through the circulation pipeline; a second mass transfer intensifier is arranged near the outlet of the circulation pipeline, the second mass transfer intensifier is connected with the gas inlet pipeline, the gas-phase raw materials in the gas inlet pipeline are treated by the second mass transfer intensifier and then enter the circulation pipeline, so that the mass transfer effect between the gas-phase raw materials and the liquid-phase raw materials is enhanced; the product outlet is higher than the outlet of the circulation pipeline in the vertical direction and is below the liquid surface of the oxidation reactor in the vertical direction.

3. The ethylbenzene potentiated oxidation reaction system according to claim 2, characterized in that, a baffle is arranged in the oxidation reactor, the top of the baffle is higher than the liquid surface of the oxidation reactor in the vertical direction, the distance between the bottom of the baffle and the bottom of the inner cavity of the oxidation reactor is a preset distance, a circulation channel is formed between the baffle and the side wall of the oxidation reactor, and the outlet of the circulation pipeline is communicated with the circulation channel.

4. The ethylbenzene potentiated oxidation reaction system according to claim 3, characterized in that, the distance between the second mass transfer intensifier and the inner wall of the oxidation reactor is smaller than the distance between the baffle and the inner wall of the oxidation reactor, and the distance between the baffle and the inner wall of the oxidation reactor is smaller than the distance between the baffle and the first mass transfer intensifier; preferably, the second mass transfer intensifier is arranged at the outlet of the circulation pipeline; preferably, the side of the baffle close to the side wall of the oxidation reactor is sequentially provided with a plurality of protrusions from top to bottom.

5. The ethylbenzene potentiated oxidation reaction system of claim 2, wherein, the number of the first mass transfer intensifiers is multiple, and the multiple first mass transfer intensifiers are all lower than the product outlet in the vertical direction; preferably, the multiple first mass transfer intensifiers are sequentially arranged from top to bottom in the vertical direction; preferably, the outlets of the multiple first mass transfer intensifiers are downward.

6. The ethylbenzene potentiated oxidation reaction system according to claim 2, characterized in that, a second heat exchanger is arranged on the circulation pipeline, and the materials in the circulation pipeline are circulated to the oxidation reactor after heat exchange through the second heat exchanger; Preferably, a circulating pump is arranged on the circulating pipeline, and located in front of the second heat exchanger along the direction of liquid flow in the circulating pipeline.

7. The ethylbenzene potentiated oxidation reaction system of claim 1, wherein, The product outlet is arranged at the lower part of the oxidation reactor, the liquid inlet pipeline is communicated with the upper part of the oxidation reactor, and the liquid inlet pipeline is lower than the liquid level of the oxidation reactor in the vertical direction; The number of the first enhanced mass transfer units is multiple, and the multiple first enhanced mass transfer units are arranged in sequence in the vertical direction between the liquid inlet pipeline and the product outlet. Preferably, the outlets of the multiple first enhanced mass transfer units are upward.

8. The ethylbenzene potentiated oxidation reaction system according to any one of claims 1 to 7, characterized by, The number of the heat exchange pipelines is multiple, and the multiple heat exchange pipelines are arranged in sequence from top to bottom.

9. The ethylbenzene potentiated oxidation reaction system according to any one of claims 1 to 7, characterized by that, Multiple layers of the baffles are arranged in the oxidation reactor in a staggered manner from top to bottom, and the multiple layers of the baffles are located below the liquid level of the oxidation reactor.

10. A process for the intensive oxidation of ethylbenzene, characterized in that The method adopts the system according to any one of claims 1-9, and the method comprises: After the gas-phase raw material is broken into micron-sized micro-bubbles by the enhanced mass transfer, the gas-phase raw material is mixed with the liquid-phase raw material to perform the oxidation reaction. The gas-phase raw material is air or oxygen, and the liquid-phase raw material is ethylbenzene.

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