Method for continuously oxidizing olefin wax with pure oxygen based on microchannel reactor

Abstract

The invention discloses a method for continuously oxidizing olefin wax by pure oxygen based on a micro-channel reactor, the micro-channel reactor comprises a plurality of gas-liquid mixers and a plurality of reinforced mixing micro-channel reactors, and two adjacent reinforced mixing micro-channel reactors are connected through the gas-liquid mixers; the method comprises the following steps: melting olefin wax, introducing the olefin wax into a microchannel reactor, injecting pure oxygen into a reinforced mixing microchannel reactor in sections by adopting a gas-liquid mixer, filling the reinforced mixing microchannel reactor with a triangular spiral filler and a glass bead material with two-stage sizes, and in the reaction process, enabling the volume concentration of oxygen to be always lower than 25% and the reaction temperature to be 100-180 DEG C, the pressure is 0-2 MPa. On the basis of the micro-channel reactor, an efficient and safe olefin wax pure oxygen oxidation process is realized through oxygen segmented injection and a safety control strategy.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of organic chemical synthesis, in particular to a method for continuous oxidation of olefin wax based on a micro-channel reactor with pure oxygen. BACKGROUND

[0002] Oxidized olefin wax is a waxy substance obtained by oxidizing olefin polymerization. By introducing oxygen-containing functional groups, the chemical modification of olefin wax compounds is performed to enhance functions such as polarity, adhesion, emulsification, lubricity, dispersibility, and chemical reactivity, while also enhancing environmental protection and multi-functionality. It is commonly used in plastic processing lubricants, coating additives, packaging materials, and has a wide application prospect in various industrial fields.

[0003] The modification methods of oxidized olefin wax can be roughly divided into graft modification and oxidation modification. The application of graft modification is narrow, and different grafting groups are directed at different directions. Oxidation modification improves the properties of olefin wax by introducing some polar groups, which can simply improve the application of olefin wax in a polar environment. Therefore, it is of great significance to study the process of simple oxidation modification of olefin wax.

[0004] The current relatively mature oxidation of olefin wax is a batch reactor production process. A method for co-oxidation of polyethylene wax, polypropylene wax and petroleum wax is disclosed in Chinese patent CN101082000A. A catalyst is used, and a compressor is started to inject oxygen, air or oxygen-containing gas into a batch raw material tank. Co-oxidation is achieved by heating and stirring.

[0005] Among them, the pure oxygen oxidation process has the following advantages: it can provide high concentration of oxidizing agent, thereby significantly improving the reaction rate and efficiency; due to the high reactivity of oxygen, the selectivity of the reaction can be enhanced, the generation of by-products can be reduced, and the yield and purity of the target product can be improved; in some cases, the use of pure oxygen can avoid the dilution effect of inert gases such as nitrogen in air on the reaction, further improving the reaction efficiency; in addition, pure oxygen oxidation process helps to achieve more precise temperature control, reduces the risk of side reactions and safety risks caused by local overheating, and improves the safety of the production process; at the same time, pure oxygen oxidation can also reduce the complexity and cost of tail gas treatment, as the amount of waste gas generated is relatively small and the composition is simple, which is conducive to environmental protection and efficient use of resources.

[0006] However, the use of pure oxygen as an oxidizing agent in traditional olefin wax oxidation processes faces multiple challenges: (1) pure oxygen is prone to combustion or explosion under high temperature and high pressure, and the local concentration of oxygen in batch reactors is too high, which poses a significant risk; (2) the low solubility of oxygen leads to low gas-liquid two-phase mass transfer efficiency, and the reaction rate is limited by oxygen diffusion; (3) it is difficult to accurately control the distribution of oxygen in traditional reactors, which can easily generate peroxides or deep oxidation by-products.

[0007] The high specific surface area and high-efficiency mixing characteristics of the micro-channel reactor can optimize gas-liquid mass transfer, and a method for synthesizing polyethylene wax by oxidation is disclosed in Chinese Patent No. CN110172109A, which uses an arrow-shaped micro-reactor system for continuous oxidation reaction, and the reaction time is shortened, but due to the size limitation of the pipeline, the pressure of the material with high viscosity increases suddenly, which is easy to block and difficult to clean.

[0008] Therefore, it is of important theoretical significance and application value to develop an intrinsically safe green oxidation process, i.e., a safe and efficient oxidation process using air or oxygen as an oxidant. The micro-reactor has high-efficiency mixing, high mass and heat transfer efficiency, and precise adjustment of reaction temperature and residence time, which can effectively control the oxidation reaction. At the same time, the micro-reactor has the characteristics of low liquid holdup and high intrinsic safety of the process, so using the micro-reactor is an effective means to solve the problems of traditional oxidation processes, such as high risk, low mass and heat transfer, poor selectivity, and low energy efficiency.

[0009] Therefore, it is necessary to develop a method for continuous oxidation of olefin wax based on a micro-channel reactor. SUMMARY

[0010] To solve the above technical problems, the purpose of the present application is to provide a method for continuous oxidation of olefin wax based on a micro-channel reactor. The present application is based on a micro-channel reactor, and realizes an efficient and safe olefin wax pure oxygen oxidation process through stepwise injection of oxygen and safety control strategy.

[0011] To achieve the above technical purpose and achieve the above technical effect, the present application realizes the following technical scheme:

[0012] The present application provides a method for continuous oxidation of olefin wax based on a micro-channel reactor, the micro-channel reactor comprising a plurality of gas-liquid mixers and a plurality of enhanced mixing micro-channel reactors, and the adjacent two enhanced mixing micro-channel reactors are connected through the gas-liquid mixer; the method melts the olefin wax and passes it into the micro-channel reactor, and uses the gas-liquid mixer to inject pure oxygen into the enhanced mixing micro-channel reactor in stages, the enhanced mixing micro-channel reactor is filled with two-stage size triangular spiral fillers and glass microbeads, the oxygen volume concentration is always less than 25% during the reaction, the reaction temperature is 100-180℃, and the pressure is 0-2MPa.

[0013] Further, the pure oxygen is injected in three stages, and the flow ratio of each stage is 1:2:1.

[0014] Further, the olefin wax comprises 1-eicosene, 1-docosene and 1-tetracosene with a content of ≥98wt%.

[0015] Furthermore, the gas-liquid mixer is a Venturi tube structure, which includes an inlet section, a contraction section, a throat section and a diffusion section.

[0016] Furthermore, the gas-liquid mixer is provided with an air inlet for introducing pure oxygen and a liquid inlet for introducing olefin wax.

[0017] Furthermore, the enhanced mixing microchannel reactor is a cylindrical tube structure, the interior of which is filled with 1.5-2 mm triangular spiral fillers and mixed reinforcement materials, and the mixed reinforcement materials are 0.1-1.0 mm glass microbeads.

[0018] Furthermore, the microchannel reactor also includes a heat-conducting structure, which is formed by pressing two heat-conducting plates together. A mixing reactor placement position is provided in the heat-conducting structure, and the enhanced mixing microchannel reactor is placed in the mixing reactor placement position.

[0019] The technical effects of the present invention are:

[0020] (1) The present invention can achieve efficient oxidation reaction at a relatively low oxygen volume concentration (always below 25%) by injecting pure oxygen in stages, thus avoiding the risk of excessively high local oxygen concentration and improving the utilization rate of oxygen, thereby increasing the reaction rate and the yield of the target product and reducing the generation of by-products.

[0021] (2) The present invention effectively reduces the possibility of pure oxygen causing combustion or explosion under high temperature and pressure by controlling the oxygen volume concentration to always be lower than 25%, and combines the low liquid holdup, efficient mixing, and precise temperature and pressure control of the microchannel reactor, thereby significantly improving the intrinsic safety of the process.

[0022] (3) The present invention utilizes the high specific surface area and efficient mixing characteristics of the microchannel reactor to significantly improve the gas-liquid two-phase mass transfer efficiency, overcome the mass transfer limitations caused by the low solubility of oxygen in traditional reactors, and enable the reaction to proceed more rapidly.

[0023] (4) The present invention adopts a microchannel reactor for the oxidation process, which can accurately adjust parameters such as reaction temperature, pressure and material flow rate, ensuring that the reaction is carried out under optimal conditions, thereby improving the quality and stability of the product.

[0024] (5) The present invention reduces the emission of unreacted oxygen and other by-products in the tail gas by precisely controlling the reaction conditions and improving the utilization rate of oxygen, thereby reducing the complexity and cost of tail gas treatment and being more beneficial to environmental protection. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] Figure 1 The diagram is a partial structural diagram of a system for implementing the method of continuous oxidation of olefin wax with pure oxygen according to the present invention.

[0026] Figure 2 Structure diagram of gas-liquid mixer in micro-channel reactor of the present application.

[0027] Figure 3 Structure diagram of gas-liquid mixer in micro-channel reactor of the present application.

[0028] Figure 4 Structure diagram of gas-liquid mixer in micro-channel reactor of the present application.

[0029] Figure 5 Structure diagram of gas-liquid mixer in micro-channel reactor of the present application.

[0030] In the figure, 1: liquid inlet, 2: gas inlet, 3: preheater, 4: feed pump, 5: gas-liquid mixer, 51: inlet section, 52: contraction section, 53: throat, 54: diffusion section, 6: enhanced mixing micro-channel reactor, 7: heat-conducting plate, 71: mixing reactor placement site, 8: gas-liquid separation tank. DETAILED DESCRIPTION

[0031] The preferred embodiments of the present application are described in detail below with reference to the accompanying drawings, so that the advantages and features of the present application can be more easily understood by those skilled in the art, and the scope of protection of the present application can be more clearly defined.

[0032] The present application provides a method for continuous oxidation of olefin wax based on pure oxygen in a micro-channel reactor, the micro-channel reactor comprising a plurality of gas-liquid mixers and a plurality of enhanced mixing micro-channel reactors, two adjacent enhanced mixing micro-channel reactors being connected by a gas-liquid mixer; the method melts the olefin wax and then passes it into the micro-channel reactor, uses the gas-liquid mixer to inject pure oxygen into the enhanced mixing micro-channel reactor in sections, fills the enhanced mixing micro-channel reactor with two-stage size triangular spiral fillers and glass beads, the oxygen volume concentration is always less than 25% during the reaction, the reaction temperature is 100-180℃, and the pressure is 0-2MPa.

[0033] Preferably, the pure oxygen is injected in three sections, and the flow rate ratio of each section is 1:2:1.

[0034] The olefin wax comprises 1-eicosene, 1-docosene and 1-tetracosene in a proportion of ≥98wt%.

[0035] As Figures 1 to 5A preferred embodiment of a microchannel continuous reaction system is shown, which utilizes a microchannel reactor to implement the method of the present invention for continuous oxidation of olefin wax with pure oxygen. Specifically, the microchannel continuous reaction system includes a feed system, a microchannel reaction module, a gas flow control system, a temperature control system, a pressure control system, a product collection and separation system, and a control and regulation system.

[0036] Among them, the feeding system transports gaseous raw materials and liquid raw materials into the microchannel reaction module. Figure 1 As shown, the feed system includes a gas inlet 2 and a liquid inlet 1, each of which is equipped with a preheater 3 and a feed pump 4. There are two preheaters 3 on each inlet to preheat the feedstock. The feed pump 4 controls the delivery of the molten olefin wax liquid and gas.

[0037] The microchannel reaction module includes three or more microchannel reactors connected in series. Figure 1 In the preferred embodiment shown, three microchannel reactors are connected in series. This structure allows for segmented flow of reactants, minimizing the liquid holdup in a single microchannel reactor, fundamentally eliminating the risk of explosive energy accumulation and complying with the inherent safety design principles of chemical processes.

[0038] Each microchannel reactor includes a gas-liquid mixer 5 and an enhanced mixing microchannel reactor 6. Among them, the gas-liquid mixer 5 is used for gas-liquid mixing, and it is a venturi tube structure, including an inlet section 51, a contraction section 52, a throat 53 and a diffusion section 54. The specific parameters of this preferred embodiment are as follows: the inner diameter of the inlet section 51 is 0.8mm, the angle of the contraction section 52 is 22°, the inner diameter of the throat 53 is 0.5mm, and the angle of the diffusion section 54 is 12°. The gas-liquid mixer 5 is provided with an air inlet and a liquid inlet, the air inlet is connected to the gas inlet 2, and the liquid inlet is connected to the liquid inlet 1. Among them, the enhanced mixing microchannel reactor 6 is a cylindrical tube structure with a pipe diameter of 6mm and a length of 15-20cm. The front end one-third is filled with a triangular spiral filler made of stainless steel with a side length and height of 1.5-2mm, and the rear end two-thirds is filled with a glass microbead mixed reinforcement material with a particle size of 0.5-1mm. In the gas-liquid mixer 5 with a venturi tube structure, the gas is sheared into micron-sized bubbles by the high-speed liquid in the throat 53, which increases the gas-liquid contact area by 10-100 times, and can solve the problem of low reaction efficiency caused by low dissolved oxygen content. The design of the contraction section 52, throat 53 and diffusion section 54 of the gas-liquid mixer 5 achieves efficient induced turbulent mixing through acceleration-cavitation-pressure recovery. The enhanced mixing microchannel reactor 6 is filled with 1.5-2mm triangular spiral fillers, which induce the fluid to generate vortex secondary flow, achieve secondary enhancement, extend the bubble residence time, and the oxygen utilization rate can reach 95%. The glass microbeads filled in the enhanced mixing microchannel reactor 6 can destroy the laminar boundary layer, induce the fluid to generate secondary vortex, cut the bubble droplets to the micron level, and eliminate the radial concentration gradient of the reactor to avoid incomplete local reaction.

[0039] Each microchannel reactor includes multiple gas-liquid mixers 5 and multiple enhanced mixing microchannel reactors 6. Adjacent enhanced mixing microchannel reactors 6 are connected by bends and gas-liquid mixers 5 to form a serpentine microchannel reactor. Each gas-liquid mixer 5 is connected to a gas branch flow path so that oxygen can enter the enhanced mixing microchannel reactor 6 in sections through the gas-liquid mixer 5.

[0040] Each microchannel reactor also includes a heat-conducting structure, which is formed by pressing two heat-conducting plates 7 together. A mixing reactor placement position 71 is provided in the heat-conducting structure, and the enhanced mixing microchannel reactor 6 is embedded in the mixing reactor placement position 71.

[0041] Among them, the gas flow in the microchannel reactor is controlled by the gas path control system, and the gas flow control range is 0.5-3L / min; the reaction temperature in the microchannel reactor is precisely controlled by the temperature control system, and the pressure in the microchannel reactor is controlled by the pressure control system, and the pressure control range is 0-2MPa.

[0042] More specifically, the gas flow control system includes a gas flow valve and a gas flow controller connected to the high-pressure gas cylinder. Specifically, the connections are in the order of high-pressure gas cylinder → pressure reducing valve → gas flow meter → gas flow valve → microchannel reactor, meaning the gas flow meter and gas flow valve are located on the gas inlet.

[0043] The temperature control system consists of an integrated jacket and a multifunction unit. The integrated jacket wraps around the outer surface of the heat-conducting structure and is connected to the multifunction unit. The multifunction unit is an intelligent temperature control device that integrates heating, cooling, circulation, and precise temperature control. It integrates an electric heater, refrigeration components, a magnetic pump, and other components. Its core function is to provide dynamic temperature regulation for the integrated jacket. The multifunction unit flows a medium into the integrated jacket, which uses the medium flow to heat or cool the microchannel reactor.

[0044] The control and regulation system includes a flow controller, a pressure sensor, a temperature sensor, and an automated control unit. The automated control unit receives temperature signals from the temperature sensor, flow signals from the flow sensor, and pressure signals from the pressure sensor, and then analyzes and sends instructions to dynamically adjust pressure, flow, and reaction temperature.

[0045] The product collection and separation system includes a gas-liquid separation tank 8 equipped with a high-precision liquid level sensor. The upper and lower ends of the gas-liquid separation tank 8 are connected to the gas outlet pipeline and the liquid outlet pipeline, respectively. The gas output from the gas outlet pipeline is recovered, and the outlet of the liquid outlet pipeline outputs the product.

[0046] The system is operated as follows: the control and regulation system is started and the reaction temperature, pressure, and flow parameters are set. Pure oxygen and molten olefin wax liquid feedstock are introduced through the feed system. Pure oxygen is injected into each microchannel reactor in three sections via a gas branch flow path, with the flow ratio of each section being 1:2:1. The gas flow rate is controlled by a gas flow valve on each gas branch flow path. The total flow rate of pure oxygen is controlled within a range of 0.5-3 L / min. The gas and liquid phases are evenly distributed and efficiently mixed and reacted within the microchannel reactor. The reaction products are separated and collected in a product collection and separation system. During the reaction, the control and regulation system monitors and adjusts the reaction conditions in real time.

[0047] The reaction device and application method of the present invention are further described below through specific oxidation reaction examples.

[0048] Example 1

[0049] The raw material olefin wax (composition: 1-eicosene 51%, 1-docosene 32%, 1-tetracosene 16%, other components <1%) was heated and melted, and then injected into the micro-channel reactor through a feed pump (temperature of the outlet of the feed pump 80°C) with the flow rate controlled at 30 mL / min. Oxygen (pure oxygen (purity ≥ 99.5%), room temperature) was injected into each micro-channel reactor in three sections (ratio 1:2:1) through the gas branch flow path under standard conditions. The gas flow rate was controlled through a gas flow valve on each gas branch flow path. The total flow rate of the pure oxygen was about 2.8 L / min.

[0050] The integrated jacket was injected with heat-conducting oil for heating, the inlet temperature of the heat-conducting oil was 165°C, and the outlet temperature was about 158°C. The reaction temperature was controlled at 163°C, the reaction pressure was 0.75 MPa, the raw material wax and oxygen were mixed in a gas-liquid mixer and then entered the enhanced mixing micro-channel reactor, the residence time was 4 min, and the product was detected to meet the quality standards. Among them, the front third of the enhanced mixing micro-channel reactor was filled with 1.5-2 mm triangular spiral fillers, and the back two-thirds were filled with 0.5 mm glass beads.

[0051] Final result: the acid value of the product was 36.54 mgKOH / g, and the saponification value was 70.29 mgKOH / g.

[0052] Example 2

[0053] The raw material wax (composition: 1-eicosene 46%, 1-docosene 35%, 1-tetracosene 18%, other components <1%) was heated and melted, and then injected into the micro-channel reactor through a feed pump (temperature of the outlet of the feed pump 80°C) with the flow rate controlled at 10 mL / min. Oxygen (pure oxygen (purity ≥ 99.5%), room temperature) was injected into each micro-channel reactor in three sections (ratio 1:2:1) through the gas branch flow path under standard conditions. The gas flow rate was controlled through a gas flow valve on each gas branch flow path. The total flow rate of the pure oxygen was about 2 L / min.

[0054] The integrated jacket was injected with heat-conducting oil for heating, the inlet temperature of the heat-conducting oil was 163°C, and the outlet temperature was about 159°C. The reaction temperature was 161°C, the reaction pressure was 0.6 MPa, the raw material wax and oxygen were mixed in a gas-liquid mixer and then entered the enhanced mixing micro-channel reactor, the residence time was 5 min, and the product was detected to meet the quality standards. Among them, the front third of the enhanced mixing micro-channel reactor was filled with 1.5-2 mm triangular spiral fillers, and the back two-thirds were filled with 1 mm glass beads.

[0055] Final result: the acid value of the product was 38.60 mgKOH / g, and the saponification value was 72.6 mgKOH / g.

[0056] Example 3

[0057] The raw material wax (composition: 1-eicosene 43%, 1-docosene 38%, 1-tetracosene 18%, other components <1%) was heated and melted, then injected into the micro-channel reactor (feed pump outlet temperature 80°C) at a flow rate of 7 mL / min, and oxygen (pure oxygen (purity ≥ 99.5%), room temperature) was injected into each micro-channel reactor in three sections (ratio 1:2:1) through the gas branch flow path under standard conditions. The gas flow rate was controlled by a gas flow valve on each gas branch flow path. The total flow rate of pure oxygen was about 0.5 L / min. Among them, the front third of the enhanced mixing micro-channel reactor was filled with 1.5-2 mm triangular spiral packing, and the back two-thirds were filled with 0.5 mm glass beads.

[0058] The integrated jacket was injected with heat conduction oil for heating, the heat conduction oil inlet temperature was 163°C, the outlet temperature was about 159°C, the reaction temperature was 161°C, the reaction pressure was 0.53 MPa, the raw material wax and oxygen were mixed in the gas-liquid mixer and then entered the enhanced mixing micro-channel reactor, the residence time was 6 min, and the product met the quality standards after detection.

[0059] Final result: product acid value 41.25 mgKOH / g, saponification value 83.57 mgKOH / g.

[0060] Comparative Example 1

[0061] 182.50 g of olefin wax (composition: 1-eicosene 51%, 1-docosene 32%, 1-tetracosene 16%, other components <1%) was added to a 500 mL autoclave, heated and melted, and the temperature was controlled at 160°C. After the raw material was completely melted and the temperature was stable, oxygen was slowly injected, 2 L of oxygen was initially injected, and then 5-10 mL / min of oxygen was added at a flow rate. An oxygen concentration sensor was set, with an alarm threshold of 8%vol, and the reaction was carried out for 8 h. The product met the quality standards after detection. The product acid value was 31.26 mgKOH / g, and the product was slightly yellow.

[0062] Comparative Example 2

[0063] 186.34 g of raw material wax (composition: 1-eicosene 46%, 1-docosene 35%, 1-tetracosene 18%, other components <1%) was added to a 500 mL autoclave, heated and melted, and the temperature was controlled at 160°C. After the raw material was completely melted and the temperature was stable, oxygen was slowly injected (pure oxygen (purity ≥ 99.5%), 2 L of oxygen was initially injected, and then 5-10 mL / min of oxygen was added at a flow rate according to the actual temperature change. An oxygen concentration sensor was set (alarm threshold 8%vol), and the reaction was carried out for 6.5 h. The product met the quality standards after detection. The product acid value was 27.06 mgKOH / g, and the product was slightly yellow.

[0064] It can be seen from the comparison of the examples and the comparative examples that the method of the present application is based on a micro-channel reactor, the micro-channel reactor has the advantages of high specific surface area, high heat transfer efficiency, high mixing efficiency, etc., can realize efficient gas-liquid mixing and heat transfer, makes the reaction more sufficient and uniform, and is beneficial to improve the selectivity and quality of the product. The present application adopts three-stage injection of oxygen, this fine control mode of segmented injection can better adjust the contact and reaction of oxygen and raw material wax, makes the oxidation reaction more sufficient and orderly, thereby improving the acid value and ketone selectivity of the product.

[0065] It is apparent to those skilled in the art that the present application is not limited to the details of the foregoing exemplary embodiments, and that the present application can be carried out in other specific forms without departing from the spirit or essential characteristics of the present application. Therefore, it is to be understood that the embodiments are to be considered in all respects as illustrative and not restrictive, and the scope of the present application is to be determined by the appended claims rather than the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are to be embraced therein.

[0066] Furthermore, it should be understood that although the present specification is described in terms of embodiments, not every embodiment according to the present application requires every embodiment feature described. This specification describes a number of embodiments, and these can be implemented individually or in any combination.

Claims

1. A method for continuous oxidation of olefin wax with pure oxygen based on a microchannel reactor, characterized in that: The microchannel reactor comprises a plurality of gas-liquid mixers and a plurality of enhanced mixing microchannel reactors, and two adjacent enhanced mixing microchannel reactors are connected via the gas-liquid mixers. The method melts olefin wax and introduces it into the microchannel reactor, and injects pure oxygen into the enhanced mixing microchannel reactor in sections by using the gas-liquid mixer. The enhanced mixing microchannel reactor is filled with triangular spiral fillers of two levels of size and glass microbead materials. During the reaction, the volume concentration of oxygen is always lower than 25%, the reaction temperature is 100-180°C, and the pressure is 0-2MPa.

2. The method for continuous oxidation of olefin wax by pure oxygen based on microchannel reactor according to claim 1, wherein The pure oxygen is injected in three sections, and the flow ratio of each section is 1:2:

1.

3. The method for continuous oxidation of olefin wax by pure oxygen based on microchannel reactor according to claim 1, wherein The olefin wax includes 1-eicosene, 1-docosene and 1-tetracosene in an amount of ≥98 wt%.

4. The method for continuous oxidation of olefin wax by pure oxygen based on microchannel reactor according to claim 1, wherein The gas-liquid mixer is a venturi tube structure, which includes an inlet section, a contraction section, a throat section and a diffusion section.

5. The method for continuous oxidation of olefin wax with pure oxygen based on microchannel reactor according to claim 1, wherein The gas-liquid mixer is provided with an air inlet for introducing pure oxygen and a liquid inlet for introducing olefin wax.

6. The method for continuous oxidation of olefin wax with pure oxygen based on microchannel reactor according to claim 1, characterized in that, The enhanced mixing microchannel reactor is a cylindrical tube structure, the interior of which is filled with 1.5-2 mm triangular spiral fillers and mixed reinforcement materials, wherein the mixed reinforcement materials are 0.1-1.0 mm glass microbeads.

7. The method for continuous oxidation of olefin wax with pure oxygen based on a microchannel reactor according to claim 1, wherein The microchannel reactor also includes a heat-conducting structure, which is formed by pressing two heat-conducting plates together. A mixing reactor placement position is provided in the heat-conducting structure, and the enhanced mixing microchannel reactor is placed in the mixing reactor placement position.

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