Pilot plant for producing fulvic acid by pyrolysis method

Abstract

The utility model discloses a pilot plant for producing fulvic acid by a pyrolysis method. The pilot plant comprises a conduction oil boiler, a grinding machine, a reaction kettle, a sleeve cooler, a buffer tank, a circulating cooling tower and a circulating cooling water pump, wherein the heat-conducting oil boiler is circularly connected with the reaction kettle; the grinding machine is sequentially connected with the reaction kettle and the buffer tank; the sleeve cooler is arranged on a pipeline between the reaction kettle and the buffer tank in a sleeving manner; the sleeve cooler is further connected with a circulating cooling tower, a circulating cooling water pump and a buffer tank in sequence; and the buffer tank is also respectively connected with the sleeve cooler and the circulating cooling tower.

Description

Technical Field

[0001] The utility model relates to the technical field of garbage treatment, and more specifically, to a pilot plant for producing fulvic acid by pyrolysis method. Background Technique

[0002] Wet garbage refers to the garbage generated in residents' daily life, food processing, catering services, unit meal supply and other activities. It is characterized by high water content and high organic matter content, and is easy to rot and produce stench, threatening the urban living environment and residents' health.

[0003] According to the differences in the actual treatment plants for different collection systems and the component characteristics of garbage, wet garbage is divided into two categories: kitchen waste and catering waste.

[0004] Kitchen waste refers to the kitchen waste peels generated after classification in residential areas and farmers' markets.

[0005] Catering waste refers to the food residues and food processing waste generated in food processing, catering services, unit meal supply and other activities outside residents' daily life.

[0006] At present, the complexity of the composition of wet garbage determines that it is difficult to complete efficient and high-value treatment and utilization using a single existing treatment technology. Therefore, one of the development ideas is to separate the components of wet garbage and comprehensively apply multiple treatment and utilization technologies.

[0007] With the continuous improvement of the technical level of wet garbage resource treatment and the increasing improvement of management regulations, in the future, various technology integration practices and innovations should continue to be carried out around wet garbage treatment, and finally the goal of efficient resource utilization and harmless treatment of wet garbage should be achieved.

[0008] Therefore, how to provide a simple and efficient method for treating wet garbage is a technical problem that needs to be solved urgently by those skilled in the art. Content of the Utility Model

[0009] In view of this, the utility model provides a pilot plant for producing fulvic acid by pyrolysis method using wet garbage as raw material.

[0010] In order to achieve the above purpose, the utility model adopts the following technical scheme:

[0011] A pilot plant for producing fulvic acid by pyrolysis method, including: a heat transfer oil boiler, a grinder, a reaction kettle, a shell-and-tube cooler, a buffer tank, a circulating cooling tower, and a circulating cooling water pump;

[0012] Wherein, the heat transfer oil boiler is connected to the reaction kettle in a circulating manner;

[0013] The grinder is connected to the reaction kettle and the buffer tank in sequence;

[0014] The sleeve cooler is sleeved on the pipeline between the reactor and the buffer tank;

[0015] The sleeve cooler is also sequentially connected to a circulating cooling tower, a circulating cooling water pump, and a buffer tank;

[0016] The buffer tank is also connected to the sleeve cooler and the circulating cooling tower respectively.

[0017] Preferably, a first regulating valve and a second regulating valve are respectively arranged on the two pipelines connecting the heat-conducting oil boiler and the reactor.

[0018] Preferably, bypasses are arranged between the heat-conducting oil boiler and the first regulating valve and between the heat-conducting oil boiler and the second regulating valve, and a third regulating valve is arranged on the bypass.

[0019] Preferably, a first control valve is arranged between the grinder and the reactor; a second control valve is arranged at the bottom of the reactor.

[0020] Preferably, a third control valve, a fourth regulating valve, and a fourth control valve are sequentially arranged between the reactor and the sleeve cooler.

[0021] Preferably, a sixth control valve is arranged between the circulating cooling water pump and the buffer tank; a fifth control valve is arranged at the bottom of the buffer tank.

[0022] Preferably, a jacket is arranged outside the reactor, and a heat-conducting oil inlet and a heat-conducting oil outlet are arranged on the jacket; the heat-conducting oil inlet is connected to the first regulating valve; the heat-conducting oil outlet is connected to the second regulating valve;

[0023] Temperature sensors and pressure sensors are arranged at the outlets of the heat-conducting oil boiler, the reactor, the circulating cooling water pump, and the buffer tank.

[0024] Preferably, the above pilot plant also includes a supporting electrical cabinet and a PLC control system.

[0025] Through the above technical solutions, compared with the prior art, the present utility model has the following beneficial effects:

[0026] 1. The humification degree of wet garbage after hydrothermal treatment is high, and a large part of the organic matter is converted into humic acid. More than 2 / 5 of the organic matter exists in the form of humic acid. Reducing the loss of organic matter and carbon source emissions helps to save energy and reduce carbon, and promotes sustainable development.

[0027] 2. The device can also be controlled by a PLC. By setting three temperature ranges and changing parameters, precise control over the temperature and time required for the organic matter reaction can be achieved. Combining with intelligent algorithm logic, automatic control of on-site equipment can be realized, reducing energy consumption and improving efficiency. The mobile phone and computer terminals support remote monitoring, facilitating real-time understanding of the system status. The remote monitoring function enables users to view real-time data, alarm information, and historical records at any time, enhancing work efficiency.

[0028] 3. A special catalyst is adopted to improve the conversion rate and yield of the product. During the reaction process, dipotassium hydrogen phosphate undergoes a decomposition reaction promoted by hydrogen ions from the self-ionization of water and then a condensation reaction with macromolecular aromatic compounds to form humic acid. This is because in the initial stage of hydrothermal treatment, relatively strong acetic acid hydrolysis and degradation and other hydrolysis reactions mainly occur as chemical reactions, and the hydrogen ions provided by dipotassium hydrogen phosphate during this period promote the rapid and intense progress of the hydrolysis reaction, thereby promoting the formation of humus. This improves the reaction efficiency, catalyst utilization rate, and product quality.

[0029] 4. Control the temperature field, pressure field, flow field, heating time, and residence time of the material in the aromatization reaction, and control the carbon element in the organic matter in the reaction product fulvic acid to achieve the goal of energy conservation and carbon reduction. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] In order to more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the following will briefly introduce the drawings required for use in the description of the embodiments or the prior art. Obviously, the drawings in the following description are only the embodiments of the present invention. For those of ordinary skill in the art, other drawings can be obtained according to the provided drawings without creative efforts.

[0031] Figure 1 It is a structural diagram of the device of the present invention;

[0032] Figure 2 It is a structural diagram of the reaction kettle of the present invention;

[0033] Among them, in the figure:

[0034] 1 - Heat transfer oil boiler; 2 - Reaction kettle; 3 - Grinder; 4 - Sleeve cooler; 5 - Buffer tank; 6 - Circulating cooling tower; 7 - Circulating cooling water pump; 11 - First regulating valve; 12 - Second regulating valve; 13 - Third regulating valve; 14 - Fourth regulating valve; 21 - First control valve; 22 - Second control valve; 23 - Third control valve; 24 - Fourth control valve; 25 - Fifth control valve; 26 - Sixth control valve. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0035] Next, the technical solutions in the embodiments of the present utility model will be clearly and completely described in conjunction with the accompanying drawings in the embodiments of the present utility model. Obviously, the described embodiments are only a part of the embodiments of the present utility model, rather than all of the embodiments. All other embodiments obtained by those of ordinary skill in the art based on the embodiments of the present utility model without creative efforts shall fall within the protection scope of the present utility model.

[0036] Embodiment 1

[0037] This embodiment provides a pilot-scale device for producing fulvic acid by pyrolysis method, including: a heat transfer oil boiler 1, a grinder 3, a reaction kettle 2, a double-pipe cooler 4, a buffer tank 5, a circulating cooling tower 6, and a circulating cooling water pump 7;

[0038] Among them, the heat transfer oil boiler 1 is connected in a cycle with the reaction kettle 2;

[0039] The grinder 3 is sequentially connected with the reaction kettle 2 and the buffer tank 5;

[0040] The double-pipe cooler 4 is sleeved on the pipeline between the reaction kettle 2 and the buffer tank 5;

[0041] The double-pipe cooler 4 is also sequentially connected with the circulating cooling tower 6, the circulating cooling water pump 7, and the buffer tank 5;

[0042] The buffer tank 5 is also respectively connected with the double-pipe cooler 4 and the circulating cooling tower 6.

[0043] In this embodiment, a first regulating valve 11 and a second regulating valve 12 are respectively arranged on the two pipelines connecting the heat transfer oil boiler 1 and the reaction kettle 2.

[0044] A bypass is arranged between the heat transfer oil boiler 1 and the first regulating valve 11 and between the heat transfer oil boiler 1 and the second regulating valve 12, and a third regulating valve 13 is arranged on the bypass.

[0045] A first control valve 21 is arranged between the grinder 3 and the reaction kettle 2; a second control valve 22 is arranged at the bottom of the reaction kettle 2.

[0046] A third control valve 23, a fourth regulating valve 14, and a fourth control valve 24 are sequentially arranged between the reaction kettle 2 and the double-pipe cooler 4.

[0047] A sixth control valve 26 is arranged between the circulating cooling water pump 7 and the buffer tank 5; a fifth control valve 25 is arranged at the bottom of the buffer tank 5.

[0048] A jacket is arranged outside the reaction kettle 2, and a heat transfer oil inlet and a heat transfer oil outlet are arranged on the jacket; the heat transfer oil inlet is connected with the first regulating valve 11; the heat transfer oil outlet is connected with the second regulating valve 12;

[0049] Temperature sensors and pressure sensors are installed at the outlets of the heat transfer oil boiler 1, the reaction kettle 2, the circulating cooling water pump 7, and the buffer tank 5.

[0050] To further optimize the above technical solution, the pilot plant also includes a supporting electrical cabinet and a PLC control system.

[0051] The PLC control system of this embodiment implements automatic control and is provided with "one-key start" and "one-key stop" functions. The equipment can be remotely monitored on the mobile terminal, achieving unattended 24-hour full monitoring and realizing intelligent control of the equipment. These are all conventional means in the prior art and will not be elaborated here.

[0052] Example 2

[0053] This embodiment provides a method for producing fulvic acid by pyrolysis, using the pilot plant for producing fulvic acid by the above pyrolysis method, which specifically includes the following steps:

[0054] S1 Pretreatment

[0055] Pour the leftovers and fruit and vegetable peels into the feed inlet of the grinder 3, and carry out grinding and refinement treatment through the grinder 3. At the same time, add clear water to adjust the slurry to a solid content of 20%; the grinder 3 is frequency conversion controlled, and by adjusting the grinding frequency (40 Hz), the particle size of the organic matter slurry can be controlled to be less than (3 mm) according to specific process requirements;

[0056] S2 Hydrothermal degradation and transformation

[0057] Add the catalyst dipotassium hydrogen phosphate to the above-mentioned obtained slurry, and the ratio of the catalyst to the material is 1:1000. Manually add the prepared organic matter slurry to the reaction kettle 2, and control the temperature of the reaction kettle through the heat transfer oil boiler 1, so that the materials in the reaction kettle 2 successively undergo anaerobic reaction, dehydration polymerization reaction, and aromatization reaction to obtain high-value humic acid; when the heat transfer oil boiler heats the materials in the reaction kettle, open the first regulating valve 11 and the second regulating valve 12, and close the third regulating valve 13. When the heated heat transfer oil flows through the jacket, it transfers heat to the reaction kettle 2, thereby heating the materials in the kettle. When the required reaction temperature is reached, the opening degrees of the 3 regulating valves can be adjusted to control the flow rate of the heat transfer oil in the inner and outer circulation channels to achieve the purpose of precise temperature control;

[0058] Among them, the temperature of the anaerobic reaction is 10-70 °C, the time is 30 min, and the pressure < 0.04 MPa; the easily degradable organic matter in the slurry mainly undergoes hydrolysis, and the macromolecular organic matter is decomposed into small molecules. For example, cellulose is decomposed into cellobiose and glucose, starch is decomposed into maltose and glucose, and protein is decomposed into short peptides and amino acids;

[0059] The temperature of the dehydration polymerization reaction is 80 - 140 °C, the time is 80 min, and the pressure is < 0.37 MPa; the intermediate product further undergoes a chemical reaction to form a more stable macromolecular substance through dehydration and polymerization;

[0060] The pressure of the aromatization reaction is 1.6 MPa, the reaction temperature is 200 °C, and the reaction time is 60 min. The macromolecular organic matter is converted into aromatic compounds through a series of dehydration and de - formaldehyde processes, and then condenses with nitrogen - containing compounds, hydrolyzed sugars (including monosaccharides, polysaccharides, etc.) and organic acids (such as furfural acid, amino acids, etc.) to form humic acid with high resource utilization value;

[0061] S3 Cooling and discharging

[0062] After most of the liquid in the reaction kettle 2 is cooled naturally, it is discharged from the discharge port of the reaction kettle 2, and the filter residue is removed by filtration to obtain a liquid humic acid product; the generated flash steam enters the buffer tank 5 through the third control valve 23, the fourth regulating valve 14, the fourth control valve 24 and the casing cooler 4 to cool down and reduce pressure to form a liquid humic acid product.

[0063] Among them, the outer jacket of the buffer tank 4 is filled with circulating cooling water. When the flash steam enters the buffer tank 4, it can be further cooled and form a liquid humic acid product when cooled.

[0064] The circulating cooling tower 6 and the circulating cooling water pump 7 provide circulating cooling water for the casing cooler 4 and the jacket.

[0065] Example 3

[0066] This example provides a method for producing fulvic acid by pyrolysis. Using the above - mentioned pilot - scale device for producing fulvic acid by pyrolysis, it specifically includes the following steps:

[0067] S1 Pretreatment

[0068] Pour the leftovers and fruit and vegetable peels into the feed inlet of the grinder 3, and conduct grinding and refinement treatment through the grinder 3. At the same time, add clear water to adjust the slurry to a solid content of 20%; the grinder 3 is frequency - controlled, and by adjusting the grinding frequency (40 Hz), the particle size of the organic matter slurry can be controlled to be less than (3 mm) according to specific process requirements;

[0069] S2 Hydrothermal degradation and transformation

[0070] Potassium hydrogen phosphate as a catalyst is added to the above-mentioned obtained slurry, and the ratio of the catalyst to the material is 1:100. The prepared organic matter slurry is manually added to the reaction kettle 2, and the temperature of the reaction kettle is controlled by the heat transfer oil boiler 1, so that the materials in the reaction kettle 2 undergo anaerobic reaction, dehydration polymerization reaction, and aromatic ring formation reaction in sequence to obtain high-value humic acid; when the heat transfer oil boiler heats the materials in the reaction kettle, the first regulating valve 11 and the second regulating valve 12 are opened, and the third regulating valve 13 is closed. When the heated heat transfer oil flows through the jacket, it transfers heat to the reaction kettle 2, thereby heating the materials in the kettle. When the required reaction temperature is reached, the opening degrees of the 3 regulating valves can be adjusted to control the flow rate of the heat transfer oil in the inner and outer circulation channels to achieve the purpose of precise temperature control;

[0071] Among them, the anaerobic reaction temperature is 10-70 °C, the time is 30 min, and the pressure < 0.04 MPa; the easily degradable organic matter in the slurry mainly undergoes hydrolysis, and the macromolecular organic matter decomposes into small molecules. For example, cellulose is decomposed into cellobiose and glucose, starch is decomposed into maltose and glucose, and protein is decomposed into short peptides and amino acids;

[0072] The dehydration polymerization reaction temperature is 80-140 °C, the time is 30 min, and the pressure < 0.37 MPa; the intermediate product further undergoes a chemical reaction to form a more stable macromolecular substance through dehydration and polymerization;

[0073] The pressure of the aromatic ring formation reaction is 1.4 MPa, the reaction temperature is 195 °C, and the reaction time is 50 min. The macromolecular organic matter is converted into aromatic compounds through a series of dehydration and de-formaldehyde reactions, and then condensed with nitrogen-containing compounds, hydrolyzed sugars (including monosaccharides, polysaccharides, etc.) and organic acids (such as furoic acid, amino acids, etc.) to form humic acid with high resource utilization value;

[0074] S3 Cooling and discharging

[0075] After most of the liquid in the reaction kettle 2 is naturally cooled, it is discharged from the discharge port of the reaction kettle 2, and the filter residue is removed by filtration to obtain a liquid humic acid product; the generated flash steam enters the buffer tank 5 through the third control valve 23, the fourth regulating valve 14, the fourth control valve 24 and the casing cooler 4 to cool down and depressurize to form a liquid humic acid product.

[0076] Among them, the outer jacket of the buffer tank 4 is filled with circulating cooling water. When the flash steam is introduced into the buffer tank 4, it can be further cooled and depressurized, and at the same time, a liquid humic acid product is formed when it meets the cold.

[0077] The circulating cooling tower 6 and the circulating cooling water pump 7 are used to provide circulating cooling water for the casing cooler 4 and the jacket.

[0078] Example 4

[0079] This embodiment provides a method for producing fulvic acid by pyrolysis. Using the pilot-scale device for producing fulvic acid by the above-mentioned pyrolysis method, it specifically includes the following steps:

[0080] S1 Pretreatment

[0081] Pour the leftovers and fruit and vegetable peels into the feed inlet of the grinder 3, and carry out grinding and refinement treatment through the grinder 3. At the same time, add clear water to adjust the slurry to a solid content of 20%. The grinder 3 is frequency conversion controlled. By adjusting the grinding frequency (40 Hz), the particle size of the organic matter slurry can be controlled to be less than (3 mm) according to specific process requirements;

[0082] S2 Hydrothermal Degradation and Transformation

[0083] Add the catalyst dipotassium hydrogen phosphate to the above-mentioned obtained slurry. The ratio of the catalyst to the material is 1:200. Manually add the prepared organic matter slurry to the reaction kettle 2, and control the temperature of the reaction kettle through the heat transfer oil boiler 1, so that the materials in the reaction kettle 2 successively carry out anaerobic reaction, dehydration polymerization reaction, and aromatization reaction to obtain high-value humic acid; when the heat transfer oil boiler heats the materials in the reaction kettle, open the first regulating valve 11 and the second regulating valve 12, and close the third regulating valve 13. When the heated heat transfer oil flows through the jacket, it transfers heat to the reaction kettle 2, thereby heating the materials in the kettle. When the required reaction temperature is reached, the opening degrees of the 3 regulating valves can be adjusted to control the flow rate of the heat transfer oil in the inner and outer circulation channels to achieve the purpose of precise temperature control;

[0084] Among them, the anaerobic reaction temperature is 10-70 °C, the time is 20 min, and the pressure < 0.04 MPa; the easily degradable organic matter in the slurry mainly undergoes hydrolysis, and the macromolecular organic matter decomposes into small molecules. For example, cellulose is decomposed into cellobiose and glucose, starch is decomposed into maltose and glucose, and protein is decomposed into short peptides and amino acids;

[0085] The dehydration polymerization reaction temperature is 80-140 °C, the time is 30 min, and the pressure < 0.37 MPa; the intermediate product further undergoes chemical reactions to form more stable macromolecular substances through dehydration and polymerization;

[0086] The pressure of the aromatization reaction is 1.3 MPa, the reaction temperature is 190 °C, and the reaction time is 60 min. The macromolecular organic matter is transformed into aromatic compounds through a series of dehydration and de-formaldehyde reactions, and then condenses with nitrogen-containing compounds, hydrolyzed sugars (including monosaccharides, polysaccharides, etc.) and organic acids (such as furfural acid, amino acids, etc.) to form humic acid with high resource utilization value;

[0087] S3 Cooling and Discharging

[0088] After most of the liquid in the reactor 2 is cooled naturally, it is discharged from the discharge port of the reactor 2, and the filter residue is removed by filtration to obtain a liquid humic acid product; the generated flash steam enters the buffer tank 5 through the third control valve 23, the fourth regulating valve 14, the fourth control valve 24 and the jacket cooler 4 to cool down and reduce the pressure to form a liquid humic acid product.

[0089] Among them, circulating cooling water is introduced into the outer jacket of the buffer tank 4. When the flash steam is introduced into the buffer tank 4, it can be further cooled and depressurized, and at the same time, a liquid humic acid product is formed when it meets the cold.

[0090] The circulating cooling tower 6 and the circulating cooling water pump 7 are used to provide circulating cooling water for the jacket cooler 4 and the jacket.

[0091] The fulvic acid obtained in Examples 2-4 is shown in Table 1 below:

[0092] Serial number Outlet pH Humic acid (%) Example 2 5.2 3.71 Example 3 5.2 3.66 Example 4 5.2 3.51

[0093] Example 5

[0094] This example provides a method for producing fulvic acid by using a pilot plant for producing fulvic acid by PLC-controlled pyrolysis method, which specifically includes the following steps:

[0095] 1. Open the PLC system page and set the material aromatization reaction temperature and aromatization reaction time;

[0096] 2. Click "Start", and the PLC automatically turns on the circulating cooling tower 6 and the circulating cooling water pump 7 according to the control logic;

[0097] 3. After crushing the material, take 1 L of slurry with a solid content of 20%, add 1 g of catalyst, and send it into the reactor 2. After the feeding is completed, click "Confirm", close the pop-up window, and then enter the heating stage;

[0098] 4. In the heating stage, the PLC automatically controls the heat transfer oil boiler 1 to heat the heat transfer oil and the material in the reactor 2. When the temperature of the reactor 2 reaches the aromatization reaction temperature, it enters the reaction stage;

[0099] 5. In the heating stage, the PLC automatically times until the reaction time ends and cools down;

[0100] 6. After the timing ends, the third regulating valve 13, the fourth regulating valve 14, the third control valve 23 and the fourth control valve 24 are automatically opened, the first regulating valve 11 and the second regulating valve 12 are closed. When the temperature of the reactor drops to room temperature, the heat transfer oil boiler 1, the circulating cooling tower 6 and the circulating cooling water pump 7 are automatically closed in sequence.

[0101] 7. Open the second control valve 22 and the fifth control valve 25 for discharging. After discharging, the materials are combined, filtered, and after solid-liquid separation, they are tested.

[0102] The various embodiments in this specification are described in a progressive manner. Each embodiment focuses on the differences from other embodiments. For the same or similar parts among the embodiments, reference can be made to each other. For the devices disclosed in the embodiments, since they correspond to the methods disclosed in the embodiments, the description is relatively simple. For the relevant parts, reference can be made to the description in the method section.

[0103] The above description of the disclosed embodiments enables those skilled in the art to implement or use the present invention. Various modifications to these embodiments will be obvious to those skilled in the art. The general principles defined herein can be implemented in other embodiments without departing from the spirit or scope of the present invention. Therefore, the present invention will not be limited to the embodiments shown herein, but will be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A pilot plant for producing fulvic acid by pyrolysis method, characterized in that, Including: Heat transfer oil boiler, grinder, reactor, shell-and-tube cooler, buffer tank, circulating cooling tower, circulating cooling water pump; Among them, the heat transfer oil boiler is connected to the reactor in a cycle; The grinder is connected to the reactor and the buffer tank in sequence; The shell-and-tube cooler is sleeved on the pipeline between the reactor and the buffer tank; The shell-and-tube cooler is also connected to the circulating cooling tower, the circulating cooling water pump and the buffer tank in sequence; The buffer tank is also connected to the shell-and-tube cooler and the circulating cooling tower respectively.

2. The pilot-scale device for producing fulvic acid by pyrolysis method according to claim 1, wherein, A first regulating valve and a second regulating valve are respectively arranged on the two pipelines connecting the heat transfer oil boiler and the reactor.

3. The pilot-scale device for producing fulvic acid by pyrolysis according to claim 2, characterized in that, A bypass is arranged between the heat transfer oil boiler and the first regulating valve and between the heat transfer oil boiler and the second regulating valve, and a third regulating valve is arranged on the bypass.

4. The pilot plant for producing fulvic acid by pyrolysis method according to claim 3, characterized in that, A first control valve is arranged between the grinder and the reactor; a second control valve is arranged at the bottom of the reactor.

5. The pilot-scale device for producing fulvic acid by pyrolysis method according to claim 4, characterized in that, A third control valve, a fourth regulating valve and a fourth control valve are arranged in sequence between the reactor and the shell-and-tube cooler.

6. The pilot plant for the production of fulvic acid by pyrolysis method according to claim 5, characterized in that, A sixth control valve is arranged between the circulating cooling water pump and the buffer tank; a fifth control valve is arranged at the bottom of the buffer tank.

7. The pilot plant for producing fulvic acid by pyrolysis according to claim 6, characterized in that, A jacket is arranged outside the reactor, and a heat transfer oil inlet and a heat transfer oil outlet are arranged on the jacket; The heat transfer oil inlet is connected to the first regulating valve; the heat transfer oil outlet is connected to the second regulating valve; Temperature sensors and pressure sensors are arranged on the heat transfer oil boiler, the reactor, the circulating cooling water pump and the buffer tank.

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