Preparation system for selectively hydrogenating high-purity oleic acid

Abstract

The utility model relates to the field of grease processing, specifically disclose a kind of preparation high-purity oleic acid selective hydrogenation preparation system, including trickle bed reactor, raw material supply system, product collection system, intelligent temperature control system and pressure control system, trickle bed reactor is divided into feed zone, grid area, spiral flow guide area and discharge area along fluid flow direction, multiple layers of grid are equipped in grid area, and the porosity and the aperture size of each layer of grid from top to bottom are gradient change respectively, catalyst bed is laid in spiral flow guide area.The utility model is through the design of the distribution of multiple layers of gradient grid and spiral flow guide in trickle bed reactor, improve catalytic effect in reaction process, utilize the accurate control of reaction temperature using multi-section independent temperature control jacket, improve reaction efficiency and product purity, cooperate with the application of pressure control system, solve the mass transfer difference, temperature uneven, the deficiency of uneven pressure of current traditional kettle type reactor.

Description

Technical Field

[0001] This utility model relates to the field of oil processing, specifically a selective hydrogenation preparation system for preparing high-purity oleic acid. Background Technology

[0002] Crude oleic acid obtained from the hydrolysis and fractionation of natural oils (such as rapeseed oil, soybean oil, and palm oil) usually contains a certain amount of polyunsaturated fatty acids, such as linoleic acid (C18:2, cis-9,12) and linolenic acid (C18:3, cis-9,12,15). However, the presence of linoleic acid and linolenic acid can affect the purity, thermal stability, and subsequent application performance of oleic acid. Existing technologies typically employ selective hydrogenation, which saturates some double bonds in polyunsaturated fatty acid (linoleic acid, linolenic acid) molecules (preferably hydrogenating double bonds away from the carboxyl group or conjugated double bonds), converting them into monounsaturated oleic acid. Simultaneously, it avoids saturating the double bonds in the oleic acid molecule (forming stearic acid), a crucial step in improving oleic acid purity. However, during operation, it has been found that traditional batch reactors suffer from poor mass transfer, uneven temperature, and uneven pressure, leading to over-hydrogenation and a significant increase in stearic acid (saturated component) content, resulting in low oleic acid purity. Furthermore, subsequent purification processes such as freeze fractionation are required, leading to high energy consumption, cumbersome operation, and hindering smooth production.

[0003] Therefore, this application specifically proposes a selective hydrogenation preparation system for high-purity oleic acid. Summary of the Invention

[0004] The purpose of this invention is to provide a selective hydrogenation system for preparing high-purity oleic acid. This system integrates a trickle-bed reactor with a grid zone and a spiral flow guiding zone, along with a raw material supply system, a product collection system, an intelligent temperature control system, and a pressure control system. It is used for the selective hydrogenation of oleic acid to prepare high-purity oleic acid. The multi-layer gradient grid distribution and spiral flow guiding design ensure uniform distribution of oleic acid and hydrogen in the catalyst bed, improving reaction efficiency and the purity of the high-purity oleic acid. It effectively solves the problems of channeling and short-circuiting in the catalyst bed. The use of multi-segment independent temperature control jackets achieves precise control of the reaction temperature, improving reaction efficiency and product purity, extending catalyst lifespan, reducing side reactions, and ensuring product quality stability. Combined with the application of a pressure control system, it overcomes the shortcomings of traditional batch reactors, such as poor mass transfer, uneven temperature, and uneven pressure.

[0005] To address the aforementioned technical problems, this invention provides a selective hydrogenation preparation system for high-purity oleic acid, comprising a trickle bed reactor, a raw material supply system, a product collection system, an intelligent temperature control system, and a pressure control system. The trickle bed reactor has a raw material inlet at its top and a product outlet at its bottom. The outlet of the raw material supply system is connected to the raw material inlet via a pipeline, and the product collection system is connected to the product outlet via a pipeline. The trickle bed reactor is divided into a feed zone, a grid zone, a spiral guide zone, and a discharge zone along the fluid flow direction. The grid zone has multiple layers of grids, with the porosity and pore size of each layer changing in a gradient from top to bottom. The spiral guide zone is lined with a catalyst bed. The outside of the trickle bed reactor has multiple temperature control jackets arranged sequentially from top to bottom. The trickle bed reactor is equipped with temperature sensors corresponding to the multiple temperature control jackets for detecting the temperature of each section. The intelligent temperature control system controls the medium temperature within each of the temperature control jackets. The pressure control system is connected to the trickle bed reactor.

[0006] Furthermore, the temperature control jacket has three sections, which are respectively located in the upper, middle and lower parts of the trickle bed reactor. The medium temperature in the upper temperature control jacket is controlled at 150-160°C, the medium temperature in the middle temperature control jacket is controlled at 160-170°C, and the medium temperature in the lower temperature control jacket is controlled at 170-180°C. Each section of the temperature control jacket is provided with an independent medium inlet and a medium outlet, and is respectively connected to a heating medium circulation system and a cooling medium circulation system.

[0007] Furthermore, the multi-layered grid is divided into an upper layer, a middle layer, and a lower layer. The porosity of the upper layer grid is 60%–70%, and the pore size is 5–8 mm. The porosity of the middle layer grid is 40%–50%, and the pore size is 3–5 mm. The porosity of the lower layer grid is 20%–30%, and the pore size is 1–3 mm.

[0008] Furthermore, each layer of the grid can be detachably installed inside the trickle bed reactor, and the grid is made of a high-strength corrosion-resistant alloy material.

[0009] Furthermore, the raw material supply system includes a hydrogen feeding system and an oleic acid feeding system. The hydrogen feeding system includes a hydrogen storage tank, a compressor, a hydrogen buffer tank, and a heat exchanger I connected in sequence via pipelines. The heat exchanger I is connected to the raw material inlet via a conveying pipeline I. The oleic acid feeding system includes an oleic acid tank, a heat exchanger II, a dryer, and a heat exchanger III connected in sequence via pipelines. The heat exchanger III is connected to the pipeline in front of the inlet of the heat exchanger I via a conveying pipeline II.

[0010] Furthermore, the product collection system includes a hydrogen-oil separator, a cooler, a degassing tank, a filter, and a finished product storage tank connected in sequence by pipelines. The product outlet is connected to the heat exchange inlet of the heat exchanger through a third conveying pipeline, and the heat exchange outlet of the heat exchanger is connected to the hydrogen-oil separator through a fourth conveying pipeline.

[0011] Furthermore, a spiral guide plate is provided within the spiral guide zone.

[0012] Furthermore, the surface of each layer of the grille is treated with sandblasting or chemical etching.

[0013] Furthermore, the pressure control system includes a pressure sensor and a pressure relief valve. The pressure sensor is installed on the trickle bed reactor, the trickle bed reactor is equipped with a pressure relief pipe, and the pressure relief valve is installed on the pressure relief pipe.

[0014] Furthermore, the middle layer of the grille has corrugated protrusions, and the height of the protrusions is 0.5 to 1 mm.

[0015] The beneficial effects of this utility model are: This invention relates to a selective hydrogenation system for preparing high-purity oleic acid. It integrates a trickle-bed reactor with a gridded zone and a spiral flow guiding zone, along with a raw material supply system, a product collection system, an intelligent temperature control system, and a pressure control system. This system is used for the selective hydrogenation of oleic acid to produce high-purity oleic acid. The multi-layered gradient grid distribution and spiral flow guiding design ensure uniform distribution of oleic acid and hydrogen in the catalyst bed, improving reaction efficiency and the purity of the high-purity oleic acid. It effectively solves the problems of channeling and short-circuiting in the catalyst bed. The use of multi-segment independent temperature control jackets achieves precise control of the reaction temperature, improving reaction efficiency and product purity, extending catalyst lifespan, reducing side reactions, and ensuring product quality stability. Combined with the application of a pressure control system, it overcomes the shortcomings of traditional batch reactors, such as poor mass transfer, uneven temperature, and uneven pressure.

[0016] The selective hydrogenation preparation system for high-purity oleic acid of this invention, through gradient porosity and pore size design, can effectively achieve rapid dispersion, uniform distribution and fine constraint of fluid, prevent channeling phenomenon, and improve catalyst utilization and reaction efficiency. Attached Figure Description

[0017] To more clearly illustrate the technical solution of this utility model, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0018] Figure 1 This is a schematic diagram of the process for preparing high-purity oleic acid by selective hydrogenation in this embodiment; Figure 2 This is a schematic diagram of the trickle bed reactor structure of the selective hydrogenation preparation system for high-purity oleic acid in this embodiment; In the diagram: 1-Trickling bed reactor, 2-Raw material supply system, 3-Product collection system, 11-Feeding zone, 12-Grid zone, 13-Spiral guide zone, 14-Discharge zone, 121-Grid, 21-Hydrogen feeding system, 22-Oleic acid feeding system, 211-Hydrogen storage tank, 212-Compressor, 213-Hydrogen buffer tank, 214-Heat exchanger one, 215-Transfer pipeline one, 221-Oleic acid tank, 222-Heat exchanger two, 223-Dryer, 224-Heat exchanger three, 225-Transfer pipeline two, 31-Hydrogen-oil separator, 32-Cooler, 33-Degassing tank, 34-Filter, 35-Finished product storage tank, 36-Transfer pipeline three, 37-Transfer pipeline four, 101-Raw material inlet, 102-Product outlet, 131-Spiral guide plate. Detailed Implementation

[0019] The technical solutions of the embodiments of this utility model will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of this utility model, and not all embodiments. Based on the embodiments of this utility model, all other embodiments obtained by those skilled in the art without creative effort are within the protection scope of this utility model.

[0020] In one specific embodiment of this utility model, such as Figure 1-2 As shown, a selective hydrogenation preparation system for high-purity oleic acid includes a trickle bed reactor 1, a raw material supply system 2, a product collection system 3, an intelligent temperature control system, and a pressure control system. The top and bottom of the trickle bed reactor 1 are respectively provided with a raw material inlet 101 and a product outlet 102. The discharge end of the raw material supply system 2 is connected to the raw material inlet 101 through a pipe, and the product collection system 3 is connected to the product outlet 102 through a pipe. The trickle bed reactor 1 is divided into a feed zone 11, a grid zone 12, a spiral guide zone 13, and a discharge zone 14 along the fluid flow direction. The grid zone 12 is equipped with multiple layers of grids 121, and the porosity and pore size of each layer of grids 121 change in a gradient from top to bottom. The spiral guide zone 13 is lined with a catalyst bed. The outside of the trickle bed reactor 1 is equipped with multiple temperature control jackets from top to bottom. The trickle bed reactor 1 is equipped with temperature sensors corresponding to the multiple temperature control jackets for detecting the temperature of each section. The intelligent temperature control system controls the medium temperature in each temperature control jacket. The trickle bed reactor 1 is connected to a pressure control system.

[0021] This invention relates to a selective hydrogenation system for preparing high-purity oleic acid. It integrates a trickle-bed reactor with a gridded zone and a spiral flow guiding zone, along with a raw material supply system, a product collection system, an intelligent temperature control system, and a pressure control system. This system is used for the selective hydrogenation of oleic acid to produce high-purity oleic acid. The multi-layered gradient grid distribution and spiral flow guiding design ensure uniform distribution of oleic acid and hydrogen in the catalyst bed, improving reaction efficiency and the purity of the high-purity oleic acid. It effectively solves the problems of channeling and short-circuiting in the catalyst bed. The use of multi-segment independent temperature control jackets achieves precise control of the reaction temperature, improving reaction efficiency and product purity, extending catalyst lifespan, reducing side reactions, and ensuring product quality stability. Combined with the application of a pressure control system, it overcomes the shortcomings of traditional batch reactors, such as poor mass transfer, uneven temperature, and uneven pressure.

[0022] Specifically, in this embodiment, the temperature control jacket (not shown in the figure) has three sections, which are respectively arranged in the upper, middle and lower parts of the trickle bed reactor 1. The temperature of the medium in the upper temperature control jacket is controlled at 150-160°C to maintain the initial progress of the hydrogenation reaction; the temperature of the medium in the middle temperature control jacket is controlled at 160-170°C to allow the hydrogenation reaction to proceed further; and the temperature of the medium in the lower temperature control jacket is controlled at 170-180°C to improve selectivity and avoid over-hydrogenation. In this embodiment, each temperature control jacket has a double-layer structure. The inner layer is tightly attached to the outer wall of the trickle bed reactor, and a closed fluid channel is formed between the outer and inner layers for introducing heating or cooling media. Each temperature control jacket has an independent media inlet and outlet, and is connected to a heating media circulation system and a cooling media circulation system, respectively. A high-precision temperature sensor is installed inside the reactor corresponding to each jacket to monitor the reaction temperature in real time and transmit the data to the intelligent temperature control system. The intelligent temperature control system uses a PID control algorithm to precisely adjust the heating or cooling power of each jacket according to the difference between the set temperature and the actual monitored temperature, achieving precise control of the reaction temperature with an accuracy of ±0.5℃.

[0023] In this embodiment, the multi-layered grid 121 is divided into an upper layer, a middle layer, and a lower layer. The porosity of the upper grid 121 is 60% to 70%, and the pore size is 5 to 8 mm. The upper grid can effectively reduce the resistance of fluid entering the catalyst bed through its larger porosity and pore size, so that the raw materials can be quickly dispersed into the catalyst bed, improve the contact efficiency between the raw materials and the catalyst, and reduce the mass transfer resistance. The middle layer of the grid 121 has a porosity of 40%–50% and a pore size of 3–5 mm. This middle layer of the grid serves as a transition and further adjusts the fluid distribution. By gradually reducing the porosity and pore size, it initially constrains and rectifyes the fluid dispersed from the upper layer, making the fluid velocity and flow rate distribution more uniform, thus preparing for the fine processing of the lower layer of the grid. In addition, corrugated protrusions (not shown in the figure) can be processed on the middle layer of the grid, and the height of these protrusions is 0.5–1 mm. The corrugations further optimize the fluid distribution by disturbing the fluid. The lower grid 121 has a porosity of 20% to 30% and a pore size of 1 to 3 mm. This lower grid is the key layer for achieving fine constraint and uniform distribution of fluid. By utilizing its tiny pores and pore size, it can strictly screen and rectify the fluid, effectively prevent channeling, and ensure that the fluid passes through the catalyst bed at a uniform flow rate and volume, so as to give full play to the activity of the catalyst and improve reaction efficiency and product quality.

[0024] Specifically, such as Figure 2 As shown, the grid in this embodiment has four layers: the upper layer includes the top layer; the middle layer includes the middle two layers; and the lower layer includes the bottom layer. For example, the upper layer has a porosity of 60% and a pore size of 6 mm; the first layer of the middle layer has a porosity of 50% and a pore size of 5 mm; the next layer of the middle layer has a porosity of 40% and a pore size of 4 mm; and the lower layer has a porosity of 30% and a pore size of 3 mm. Each layer, through a gradient-designed grid, achieves precise control of fluid distribution.

[0025] In this embodiment, each layer of grid 121 can be detachably installed in the trickle bed reactor 1. Here, the adjacent two layers of grid are connected by detachable flanges, which makes the disassembly and installation process simple and quick. The specific connection method can be achieved using existing technology, so it will not be described in detail. When it is necessary to maintain the equipment or replace the catalyst, the multi-layer gradient grids connected by the flanges can be disassembled to facilitate the operation inside the reactor. Specifically, the grating 121 is made of a high-strength corrosion-resistant alloy material. The alloy material can preferably be a special stainless steel alloy containing elements such as molybdenum, chromium, and nickel, with a tensile strength of over 800 MPa. It can still maintain good mechanical properties and chemical stability in high-temperature and highly corrosive environments. In addition, to further improve the uniformity of fluid distribution, the surface of each layer of grid 121 is treated with sandblasting or chemical etching. This treatment method can increase the roughness of the grid surface, thereby generating more turbulence and disturbance when the fluid passes through the grid, so that the fluid can be more uniformly dispersed in the catalyst bed. Through the application of surface treatment technology, the uniformity of fluid distribution is greatly improved, and the reaction efficiency is further improved.

[0026] In this embodiment, a spiral guide plate 131 is provided in the spiral guide zone 13. Specifically, the spiral guide plate spirals upward around the inner wall of the trickle bed reactor. A catalyst bed, such as a selective hydrogenation catalyst like Pt-Sn / Al2O3, is distributed on the spiral guide plate. Under the guidance of the spiral guide plate, the fluid flows spirally downward along the inner wall of the reactor, forming a spiral flow field. This flow field can disperse the fluid kinetic energy, reduce the direct impact of the fluid on the catalyst, make the force of the fluid on the catalyst bed uniform, maintain the stability of the bed, and at the same time reduce the disordered collision between catalyst particles, prevent particle agglomeration, and protect the catalyst activity and structural integrity.

[0027] like Figure 1 As shown, in this embodiment, the raw material supply system 2 includes a hydrogen feeding system 21 and an oleic acid feeding system 22. The hydrogen feeding system 21 includes a hydrogen storage tank 211, a compressor 212, a hydrogen buffer tank 213 and a heat exchanger 214 connected in sequence by pipelines. The heat exchanger 214 is connected to the raw material inlet 101 through a conveying pipeline 215. The oleic acid feeding system 22 includes an oleic acid tank 221, a heat exchanger 222, a dryer 223 and a heat exchanger 224 connected in sequence by pipelines. The heat exchanger 224 is connected to the pipeline in front of the inlet of the heat exchanger 214 through a conveying pipeline 225. The product collection system 3 includes a hydrogen-oil separator 31, a cooler 32, a degassing tank 33, a filter 34, and a finished product storage tank 35, which are connected in sequence by pipelines. The product outlet 102 is connected to the heat exchange inlet of the heat exchanger 224 via a conveying pipeline 36, and the heat exchange outlet of the heat exchanger 224 is connected to the hydrogen-oil separator 31 via a conveying pipeline 47. This layout can improve the energy utilization rate of the heat exchanger 224 and achieve a certain energy consumption utilization purpose.

[0028] In this embodiment, the pressure control system includes a pressure sensor and a pressure relief valve (not shown in the figure). The pressure sensor is installed on the trickle bed reactor 1, and a pressure relief pipe is installed on the trickle bed reactor 1. The pressure relief valve is installed on the pressure relief pipe. The pressure sensor monitors the pressure inside the trickle bed reactor in real time. When the pressure exceeds the set value, the pressure relief valve automatically opens to release pressure, thereby improving the safety of the reaction process.

[0029] The working principle of this utility model is as follows: Hydrogen from hydrogen storage tank 211 is piped to compressor 212 to increase the pressure to about 2.0 MPa (adjusted according to production needs), and then enters hydrogen buffer tank 213. It is then mixed with oleic acid from conveying pipeline 225 (here, oleic acid from oleic acid tank 221 is piped to heat exchanger 222 to be heated to 100-110°C, then dried by dryer 223 and piped to heat exchanger 324 to be heated to 110-130°C), and then enters heat exchanger 114 to be heated to 150-160°C. Finally, it is piped to raw material inlet 101 of trickle bed reactor 1 through conveying pipeline 215. After the raw material enters the trickling bed reactor 1, it passes through a multi-layer gradient grid to achieve initial dispersion and fine distribution. Then, guided by the spiral guide plate 131, it flows spirally downward along the inner wall of the trickling bed reactor 1, and makes full contact with the catalyst on the catalyst bed to carry out selective hydrogenation reaction. During the reaction, temperature sensors corresponding to each temperature control jacket monitor the reaction temperature in real time and transmit the data to the intelligent temperature control system. The intelligent temperature control system precisely controls the heating or cooling power of each temperature control jacket according to the set temperature and the actual temperature to ensure that the reaction temperature is stable within the set range (±0.5℃). In addition, pressure sensors monitor the pressure inside the trickle bed reactor 1 in real time. When the pressure exceeds the set value, the pressure relief valve automatically opens to discharge excess gas and ensure the safe conduct of the reaction. After the reaction is complete, the product enters the heat exchanger 224 through the product outlet 102 via the conveying pipeline 36 to exchange heat with oleic acid. After heat exchange, it is conveyed through the conveying pipeline 4 to the hydrogen-oil separator 31 to separate hydrogen and oil. The product is then cooled by the cooler 32, separated by the degassing tank 33, filtered by the filter 34, and finally stored in the finished product storage tank 35 to obtain high-purity oleic acid.

[0030] The above-disclosed embodiment is merely a preferred embodiment of the present utility model and should not be construed as limiting the scope of the present utility model. Therefore, any equivalent variations made in accordance with the claims of the present utility model shall still fall within the scope of the present utility model.

Claims

1. A selective hydrogenation preparation system for high-purity oleic acid, characterized in that, The system includes a trickle bed reactor (1), a raw material supply system (2), a product collection system (3), an intelligent temperature control system, and a pressure control system. The trickle bed reactor (1) has a raw material inlet (101) at the top and a product outlet (102) at the bottom. The discharge end of the raw material supply system (2) is connected to the raw material inlet (101) through a pipe, and the product collection system (3) is connected to the product outlet (102) through a pipe. The trickle bed reactor (1) is divided into a feed zone (11), a grid zone (12), a spiral guide zone (13), and a discharge zone (14) along the fluid flow direction. The grid zone (12) is provided with multiple grids (121), and the porosity and pore size of each grid (121) from top to bottom are gradient changes. The spiral guide zone (13) is provided with a catalyst bed. The outside of the trickle bed reactor (1) is provided with multiple temperature control jackets from top to bottom. The trickle bed reactor (1) is provided with temperature sensors corresponding to the multiple temperature control jackets for detecting the temperature of each section. The intelligent temperature control system controls the medium temperature in each of the temperature control jackets. The pressure control system is connected to the trickle bed reactor (1).

2. The selective hydrogenation preparation system for high-purity oleic acid according to claim 1, characterized in that, The temperature control jacket has three sections, which are respectively located in the upper, middle and lower parts of the trickle bed reactor (1). The temperature of the medium in the upper temperature control jacket is controlled at 150-160°C, the temperature of the medium in the middle temperature control jacket is controlled at 160-170°C, and the temperature of the medium in the lower temperature control jacket is controlled at 170-180°C. Each section of the temperature control jacket is provided with an independent medium inlet and a medium outlet, and is respectively connected to a heating medium circulation system and a cooling medium circulation system.

3. The selective hydrogenation preparation system for high-purity oleic acid according to claim 1, characterized in that, The multi-layered grid (121) is divided into an upper layer, a middle layer and a lower layer. The porosity of the upper layer grid (121) is 60% to 70% and the pore size is 5 to 8 mm. The porosity of the middle layer grid (121) is 40% to 50% and the pore size is 3 to 5 mm. The porosity of the lower layer grid (121) is 20% to 30% and the pore size is 1 to 3 mm.

4. The selective hydrogenation preparation system for high-purity oleic acid according to claim 1, characterized in that, Each layer of the grid (121) can be detachably installed in the trickle bed reactor (1), and the grid (121) is made of high-strength corrosion-resistant alloy material.

5. The selective hydrogenation preparation system for high-purity oleic acid according to claim 1, characterized in that, The raw material supply system (2) includes a hydrogen feeding system (21) and an oleic acid feeding system (22). The hydrogen feeding system (21) includes a hydrogen storage tank (211), a compressor (212), a hydrogen buffer tank (213), and a heat exchanger (214) connected in sequence by pipelines. The heat exchanger (214) is connected to the raw material inlet (101) through a conveying pipeline (215). The oleic acid feeding system (22) includes an oleic acid tank (221), a heat exchanger (222), a dryer (223), and a heat exchanger (224) connected in sequence by pipelines. The heat exchanger (224) is connected to the pipeline in front of the inlet of the heat exchanger (214) through a conveying pipeline (225).

6. The selective hydrogenation preparation system for high-purity oleic acid according to claim 5, characterized in that, The product collection system (3) includes a hydrogen-oil separator (31), a cooler (32), a degassing tank (33), a filter (34), and a finished product storage tank (35) connected in sequence by pipelines. The product outlet (102) is connected to the heat exchange inlet of the heat exchanger (224) through a third conveying pipeline (36), and the heat exchange outlet of the heat exchanger (224) is connected to the hydrogen-oil separator (31) through a fourth conveying pipeline (37).

7. The selective hydrogenation preparation system for high-purity oleic acid according to claim 1, characterized in that, The spiral guide zone (13) is provided with a spiral guide plate (131).

8. The selective hydrogenation preparation system for high-purity oleic acid according to claim 1, characterized in that, The surface of each layer of the grid (121) is treated with sandblasting or chemical etching.

9. The selective hydrogenation preparation system for high-purity oleic acid according to claim 1, characterized in that, The pressure control system includes a pressure sensor and a pressure relief valve. The pressure sensor is installed on the trickle bed reactor (1), and a pressure relief pipe is installed on the trickle bed reactor (1). The pressure relief valve is installed on the pressure relief pipe.

10. The selective hydrogenation preparation system for high-purity oleic acid according to claim 3, characterized in that, The middle layer of the grille (121) has corrugated protrusions, and the height of the protrusions is 0.5 to 1 mm.

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