Continuous production system

Abstract

The invention discloses a continuous production system, which comprises: a reaction unit; the plurality of feeding units are respectively communicated with the reaction unit, each feeding unit is used for introducing different reaction raw materials into the reaction unit, and the reaction raw materials comprise solvent oil, a monomer and a catalyst; the supercharging unit is provided with an input end and an output end; the output end of the pressurizing unit is communicated with the reaction unit; the Venturi tube is provided with an input end and an output end, the input end of the Venturi tube is communicated with the reaction unit, and the output end of the Venturi tube is communicated with the input end of the pressurizing unit; the conversion unit is communicated with the Venturi tube and is used for converting a liquid branching agent into a gaseous branching agent and inputting the gaseous branching agent into the Venturi tube; the pressurizing unit is used for pressurizing gas and a gaseous modifier in the reaction unit and then conveying the gas and the gaseous modifier into the reaction unit; the reaction unit is used for heating and stirring the gaseous modifier and the reaction raw materials.

Description

Technical Field

[0001] This invention relates to the field of chemical refining technology, and in particular to a continuous production system. Background Technology

[0002] Polybutadiene rubber (PPB) is the second most produced synthetic rubber after styrene-butadiene rubber (SBR). It is generally prepared using catalysts such as nickel-based, cobalt-based, titanium-based, lithium-based, rare-earth-based, molybdenum-based, and iron-based catalysts. Different catalysts can synthesize PPB with different structures, such as rare-earth cis-butadiene rubber, meta-1,2-polybutadiene rubber, low-cis PPB, high-vinyl PPB, and liquid PPB.

[0003] Rare earth butadiene rubber has higher molecular weight, structural regularity, high linearity, narrow molecular weight distribution, and Mooney viscosity adjustable at ML 100℃ (1+4). This gives it excellent flexural strength, abrasion resistance, low rolling resistance, and better raw rubber strength and vulcanized rubber performance, making it suitable for the high-speed driving requirements of automobiles. It is widely used in tire tread and sidewall rubber and is a key rubber type for preparing high-performance green tires.

[0004] However, due to the excessively linear molecular chain of rare earth cis-butadiene rubber, its latex viscosity and transportability are relatively high, and the rubber compounding process is also quite difficult. Therefore, it is necessary to introduce branched structures into the rare earth rubber molecular chain. This is achieved by adding branching modifiers during the preparation of rare earth cis-butadiene rubber. Firstly, this reduces the hydrodynamic volume of the rare earth rubber molecular chain in solution, thereby reducing its latex viscosity. Secondly, it improves its compounding and processing performance, making it easier to incorporate materials and improve filler dispersion, thus significantly reducing the Mooney viscosity of the compound. Thirdly, the introduction of branched structures endows rare earth rubber with higher cold flow resistance, facilitating storage and transportation.

[0005] The existing technology for long-chain branching modification of rare earth cis-butadiene rubber has the following problems:

[0006] 1. The entire process of long-chain branching modification of rare earth cis-butadiene rubber is carried out in an intermittent production process. There is a lack of continuous production equipment for the long-chain branching modification reaction of rare earth cis-butadiene rubber. The discontinuous reaction process not only affects production efficiency and increases production costs, but also greatly prolongs the production cycle.

[0007] 2. Branching modifiers are generally in liquid form. The reaction between liquid branching agents and rare earth cis-butadiene rubber is often slow, and it often takes a long time for the branching agent to diffuse into the rare earth rubber molecular chain. This seriously affects the reaction efficiency and product quality of rare earth cis-butadiene rubber preparation. In contrast, gaseous branching agents diffuse into the rare earth rubber molecular chain more quickly, which can meet the reaction efficiency and product quality requirements for rare earth cis-butadiene rubber preparation. However, there are often no readily available industrial products for gaseous branching agents.

[0008] The present invention solves at least one of the above problems. Summary of the Invention

[0009] The purpose of this invention is to provide a continuous production system for the long-chain branching modification reaction of rare earth cis-butadiene rubber. Through continuous reaction production, production efficiency is improved, production costs are reduced, and the production cycle is significantly shortened.

[0010] The objective of this invention is achieved through the following technical solution:

[0011] A continuous production system, comprising:

[0012] Reaction unit;

[0013] Multiple feeding units are connected to the reaction unit, and each feeding unit is used to feed different reaction raw materials into the reaction unit, including solvent oil, monomer and catalyst.

[0014] A booster unit has an input terminal and an output terminal; the output terminal of the booster unit is connected to the reaction unit.

[0015] A venturi tube has an input terminal and an output terminal. The input terminal of the venturi tube is connected to the reaction unit, and the output terminal of the venturi tube is connected to the input terminal of the booster unit.

[0016] A conversion unit, connected to the Venturi tube, is used to convert the liquid branching agent into a gaseous branching agent and input the gaseous branching agent into the Venturi tube;

[0017] The pressurization unit is used to pressurize the gas and gaseous modifier inside the reaction unit and then deliver them into the reaction unit;

[0018] The reaction unit is used to heat and stir the gaseous modifier and the reaction raw materials.

[0019] Compared with the prior art, the beneficial effects of the present invention are as follows: The continuous production system of this application feeds different reaction raw materials into the reaction unit through multiple feeding units. The reaction unit continuously heats and stirs the reaction raw materials to cause polymerization reaction, generating rare earth cis-butadiene rubber and mixed gas. The liquid branching agent is converted into a gaseous branching agent through the conversion unit. The gaseous branching agent enters the Venturi tube under pressure. The mixed gas in the reaction unit enters the input end of the pressurization unit from the output end of the Venturi tube. At the same time, the mixed gas is pressurized by the pressurization unit. The gaseous branching agent follows the mixed gas and is sent into the reaction unit through the output end of the pressurization unit under pressure. The long-chain branching modification of rare earth cis-butadiene rubber is achieved through continuous heating and stirring in the reaction unit. By continuously feeding reaction materials through the feeding unit, continuously converting liquid branching agent into gaseous form and sending it into the Venturi tube through the conversion unit, continuously heating and stirring in the reaction unit, and continuously pressurizing through the pressurization unit, continuous production of long-chain branching modification of rare earth cis-butadiene rubber is achieved. The continuity of the chemical reaction ensures constant reaction conditions and stable product quality during the long-chain branching modification of rare earth cis-butadiene rubber, thus realizing a continuous preparation process. This improves the production efficiency of long-chain branching modification of rare earth cis-butadiene rubber, reduces production costs, and significantly shortens the production cycle.

[0020] In some possible implementations, the feeding unit includes:

[0021] The feed tank has a first end and a second end that are arranged opposite to each other along the height direction;

[0022] The second pipeline has one end connected to the first end of the feed tank and the other end used to introduce the reaction raw materials; a first valve is provided on the second pipeline.

[0023] The third pipeline has one end connected to the second end of the feed tank and the other end connected to the first port of the three-way valve. A second valve is installed on the third pipeline.

[0024] The first metering tank has a first end and a second end that are arranged opposite to each other along the height direction;

[0025] The fourth pipeline has one end connected to the second port of the three-way valve and the other end connected to the first end of the first metering tank.

[0026] The second metering tank has a first end and a second end that are arranged opposite to each other along the height direction;

[0027] The fifth pipeline has one end connected to the third port of the three-way valve and the other end connected to the first end of the second metering tank.

[0028] The sixth pipeline has one end connected to the second end of the first metering tank and the other end connected to the first interface of the four-way pipe.

[0029] The seventh pipeline has one end connected to the second end of the second metering tank and the other end connected to the second interface of the four-way pipe.

[0030] A metering pump is connected to the third port of the four-way pipe, and the fourth port of the four-way pipe is connected to the reaction unit.

[0031] The first pressure regulating pipeline has one end connected to the first end of the feed tank and the other end connected to the first interface of the tee pipe.

[0032] A second pressure regulating pipeline, one end of which is connected to the first end of the first metering tank, and the other end of which is connected to the second port of the tee pipe; and

[0033] The third pressure regulating pipeline has one end connected to the first end of the second metering tank, and the other end connected to the third interface of the tee pipe.

[0034] In some possible implementations, the feeding unit further includes:

[0035] A first support is sleeved and connected to the side wall of the first metering tank, and a first loss-in-weight scale is provided at the bottom of the first support.

[0036] The first level gauge is installed at the first end of the first metering tank and is located inside the first metering tank;

[0037] A second support is fitted and connected to the side wall of the second metering tank, and a second loss-in-weight scale is installed at the bottom of the second support; and

[0038] The second level gauge is installed at the first end of the second metering tank and is located inside the second metering tank.

[0039] In some possible implementations, the reaction unit includes:

[0040] The first reactor has a first end and a second end that are arranged opposite each other along the height direction, and a first overflow port is provided on the side wall of the first reactor;

[0041] First pipeline; one end of the first pipeline is connected to the second end of the first reactor;

[0042] Multiple feed branches, one end of each feed branch is connected to the other end of the first pipeline; the other ends of each feed branch are respectively connected to one of the feed units;

[0043] A first driving device is disposed at the first end of the first reaction vessel;

[0044] The first double-helix stirrer is located inside the first reaction vessel and is coaxially connected to the drive end of the first drive device.

[0045] The second reactor has a first end and a second end that are arranged opposite each other along the height direction, and a second overflow port is provided on the side wall of the second reactor;

[0046] A first series pipeline, one end of which is connected to the first overflow port, and the other end of which is connected to the second end of the second reactor;

[0047] The second driving device is located at the first end of the second reactor.

[0048] The second double-helix stirrer is located inside the second reactor and is coaxially connected to the drive end of the second drive device.

[0049] The third reactor has a first end and a second end that are arranged opposite each other along the height direction. The side wall of the third reactor is provided with a third overflow port. The third overflow port and the storage tank are connected through a discharge pipe. The first end of the third reactor and the Venturi tube are connected through a first bend pipe. The first end of the third reactor and the output end of the pressurization unit are connected through a second bend pipe. A fifth control valve is provided on the second bend pipe.

[0050] The second series pipeline has one end connected to the second overflow port and the other end connected to the second end of the third reactor.

[0051] A third driving device is disposed at the first end of the third reactor; and

[0052] The third double-helix stirrer is located inside the third reactor and is coaxially connected to the drive end of the third drive device.

[0053] In some possible implementations, the first bend and the venturi tube are connected via a buffer unit, the buffer unit comprising:

[0054] A buffer tank, the buffer tank having an inlet pipe and an outlet pipe inside, the buffer tank containing a buffer solution, the inlet pipe having one end connected to the first bent pipe on the outside of the buffer tank, the inlet pipe having one end located below the surface of the buffer solution on the inside of the buffer tank, the outlet pipe having one end connected to the buffer tank located above the surface of the buffer solution, and the other end of the outlet pipe connected to the inlet of the Venturi tube; and / or,

[0055] The buffer tank is provided with a first discharge port at the bottom, and a first valve is installed on the first discharge port; and / or,

[0056] A first control valve is installed on the air intake pipe;

[0057] A sixth control valve is installed on the exhaust pipe.

[0058] In some possible implementations, the buffer unit further includes a protection module, the protection module comprising:

[0059] A protective branch pipe, the two ends of which are respectively connected to the air inlet pipes on both sides of the first control valve;

[0060] A back pressure valve, which is installed on the protective branch pipe;

[0061] The second control valve is installed on the protective branch pipe on one side of the input end of the back pressure valve;

[0062] The first fine-tuning valve is installed on the protective branch pipe on one side of the output end of the back pressure valve;

[0063] A third control valve is installed on the inlet pipe downstream of the protective branch pipe along the gas flow direction; and

[0064] An vent pipe is installed on the buffer tank, and a fourth control valve is installed on the vent pipe.

[0065] In some possible implementations, the conversion unit includes:

[0066] A feeding tank has a top and a bottom arranged opposite each other along its height; the top of the feeding tank is provided with a feed inlet for feeding liquid branching agent and an air inlet for connecting to a nitrogen source; and

[0067] A heating vessel has a top and a bottom disposed opposite each other along the height direction; the heating vessel is located below the feeding tank and is used to convert the liquid branching agent into a gaseous branching agent;

[0068] The bottom of the feeding tank and the top of the heating vessel are connected by an eighth pipeline, and a first regulating valve is provided on the eighth pipeline;

[0069] The top of the feeding tank and the top of the heating vessel are connected by a fourth pressure regulating pipeline, and a second regulating valve is provided on the fourth pressure regulating pipeline;

[0070] The top of the heating vessel is connected to one end of the ninth pipeline, and the other end of the ninth pipeline is connected to the Venturi tube.

[0071] In some possible implementations, the eighth pipeline is also provided with a second on / off valve located between the first regulating valve and the bottom of the feeding tank.

[0072] In some possible implementations, the bottom of the heating vessel is provided with a discharge valve; the conversion unit further includes a first discharge pipeline, the discharge valve has a discharge port, one end of the first discharge pipeline is connected to the discharge port, the other end of the first discharge pipeline is connected to a first collection tank, and a first on / off valve is provided on the first discharge pipeline.

[0073] In some possible implementations, the conversion unit further includes:

[0074] The second discharge pipe has one end connected to the top of the heating vessel and the other end connected to the second collection tank.

[0075] The second discharge pipeline is equipped with a third on / off valve near the top of the heating vessel and a fourth on / off valve near the second collection tank; and

[0076] The third discharge pipeline has one end connected to the second discharge pipeline between the third on / off valve and the fourth on / off valve; the other end of the third discharge pipeline is connected to the first discharge pipeline between the first on / off valve and the discharge port.

[0077] A fifth shut-off valve is installed on the third discharge pipeline. Attached Figure Description

[0078] Figure 1 This is a partial structural schematic diagram of the continuous production system according to an embodiment of the present invention;

[0079] Figure 2 This is a schematic diagram of the feeding unit according to an embodiment of the present invention;

[0080] Figure 3 This is a schematic diagram of the conversion unit according to an embodiment of the present invention;

[0081] Figure 4 This is a top view of the feeding tank according to an embodiment of the present invention.

[0082] Figure reference numerals: 1. Pressurization unit; 2. Venturi tube; 3. Feed tank; 4. Second pipeline; 4a. First valve; 5. Third pipeline; 5a. Second valve; 6. Three-way valve; 7. First metering tank; 8. Fourth pipeline; 9. Second metering tank; 10. Fifth pipeline; 11. Sixth pipeline; 12. Four-way pipe; 13. Seventh pipeline; 14. Metering pump; 15. First pressure regulating pipeline; 16. Second pressure regulating pipeline; 17. Third pressure regulating pipeline; 18. First support; 19. First loss-in-weight scale; 20. First 21. Level gauge; 22. Second support; 23. Second loss-in-weight balance; 24. Second level gauge; 25. First reactor; 24a. First overflow port; 26. First pipeline; 27. Feed branch; 28. First drive unit; 29. ​​First double-helix stirrer; 30. Second reactor; 29a. Second overflow port; 31. First series pipeline; 32. Second drive unit; 33. Second double-helix stirrer; 34. Third reactor; 35. Third overflow port; 36. Discharge pipe; 37. First bend; 38. 37. Second series pipeline; 38. Third drive device; 49. Third double spiral agitator; 40. Buffer tank; 41. Air inlet pipe; 411. First control valve; 412. Third control valve; 42. Exhaust pipe; 421. Sixth control valve; 43. First discharge port; 44. Protective branch pipe; 441. Back pressure valve; 442. Second control valve; 443. First fine-tuning valve; 45. Drain pipe; 451. Fourth control valve; 46. Second bend pipe; 461. Fifth control valve; 50. Feeding tank; 51. Heating vessel ; 52. Eighth pipeline; 521. First regulating valve; 53. Fourth pressure regulating pipeline; 531. Second regulating valve; 54. Ninth pipeline; 541. Second on / off valve; 55. Discharge valve; 551. Discharge port; 56. First discharge pipeline; 561. First on / off valve; 57. Second discharge pipeline; 571. Third on / off valve; 572. Fourth on / off valve; 58. Third discharge pipeline; 581. Fifth on / off valve; 100. Feed inlet; 200. Air inlet; 300. Isobaric port; 400. Vent port. Detailed Implementation

[0083] Exemplary embodiments will now be described more fully with reference to the accompanying drawings. However, these exemplary embodiments can be implemented in many forms and should not be construed as limited to the embodiments set forth herein; rather, they are provided to make the invention more comprehensive and complete, and to fully convey the concept of the exemplary embodiments to those skilled in the art. The same reference numerals in the drawings denote the same or similar structures, and therefore repeated descriptions of them will be omitted.

[0084] The terms used to express position and direction in this invention are illustrated with reference to the accompanying drawings, but changes can be made as needed, and all such changes are included within the scope of protection of this invention.

[0085] Please refer to the following: Figures 1 to 4 As shown, the present invention provides a continuous production system for the long-chain branching modification of rare earth cis-butadiene rubber, including a reaction unit, multiple feeding units, a pressurization unit 1, a venturi tube 2, and a conversion unit.

[0086] Multiple feed units are connected to the reaction unit, and each feed unit is used to feed different reaction raw materials into the reaction unit. The reaction raw materials include solvent oil, monomers and catalysts.

[0087] The purpose of this application is to provide a continuous production system for the long-chain branching modification of rare earth cis-butadiene rubber, which is convenient for production and preparation. The specific process parameters and reaction raw materials are not within the protection scope of this application.

[0088] Obviously, the embodiments of this application do not include a method for preparing long-chain branched modification of rare earth cis-butadiene rubber. The reaction raw materials used in this application can achieve long-chain branched modification of rare earth cis-butadiene rubber under appropriate process parameters. The embodiments of this application do not protect the reaction raw materials and process parameters, as these are conventional technical means and will not be described in detail here.

[0089] Therefore, in order to facilitate the description of the working principle of the continuous production system, the reaction raw materials are described by way of example from the perspective known to those skilled in the art.

[0090] In this embodiment, the catalyst is a homogeneous rare earth catalyst, comprising four catalyst components from catalyst A to catalyst D.

[0091] Catalyst A can be a neodymium carboxylate compound, preferably one or a mixture of neodymium isooctanoate and neodymium neodecanoate or other organic acid neodymium compounds. In this embodiment, catalyst A is preferably neodymium isooctanoate and neodymium neodecanoate. Catalyst B can be one or more of alkylaluminum compounds, hydrogenated alkylaluminum compounds, or other organoaluminoxanes. In this embodiment, catalyst B is preferably triisobutylaluminum and diisobutylaluminum hydrogenate. Catalyst C can be a conjugated diene compound. In this embodiment, catalyst C is preferably butadiene and isoprene. Catalyst D can be an alkylaluminum chloride compound. In this embodiment, catalyst D is preferably diethylaluminum chloride and diisobutylaluminum chloride.

[0092] An exemplary method for preparing a homogeneous rare earth catalyst is as follows: Under argon or nitrogen protection, catalyst A, catalyst C, catalyst B, and catalyst D are added sequentially. After mixing thoroughly at 0–50°C, the temperature is raised to 20–70°C and aging continues for 10–120 min to obtain a homogeneous rare earth catalyst. The preferred molar ratio of catalyst A, catalyst B, catalyst C, and catalyst D is 1:(5–40):(5–50:(1–6):(0.1–50).

[0093] The preparation of homogeneous rare earth catalysts is a conventional technique and will not be elaborated here.

[0094] Each group of catalysts enters a corresponding feeding unit through its own storage tank, requiring a total of four feeding units.

[0095] The solvent oil is one or more of cyclohexane, cyclopentane, n-pentane, n-hexane, and n-heptane. The solvent oil enters a corresponding feeding unit through a storage tank, and a total of one feeding unit is required. In this embodiment, the solvent oil is preferably n-hexane.

[0096] There are three types of monomers: butadiene, styrene, and isoprene. Each monomer enters a corresponding feeding unit through its own storage tank, requiring a total of three feeding units.

[0097] In summary, the required reaction materials for achieving long-chain branching modification of rare earth cis-butadiene rubber include four catalysts, three monomers, and one solvent oil, totaling seven feed units.

[0098] For example, the synthesis process of rare earth cis-butadiene rubber includes: adding a homogeneous rare earth catalyst to a mixed solution of solvent oil and monomer, and then initiating the monomer polymerization reaction at a temperature range of 0–100°C for a total reaction time of 30–180 min, wherein the amount of homogeneous rare earth catalyst added is such that the molar ratio of catalyst component A to monomer is equal to 1 × 10⁻⁶. -5 ~2×10 -4 The synthesis process of rare earth butadiene rubber is a conventional technique and will not be elaborated here.

[0099] It should be noted that for different long-chain branching modification processes, the adaptability of the feed unit can be increased or decreased as the amount of reaction raw materials increases or decreases.

[0100] The booster unit 1 has an input terminal and an output terminal, and the output terminal of the booster unit 1 is connected to the reaction unit.

[0101] The venturi tube 2 has an input terminal and an output terminal. The input terminal of the venturi tube 2 is connected to the reaction unit, and the output terminal of the venturi tube 2 is connected to the input terminal of the booster unit 1.

[0102] The conversion unit is connected to the Venturi tube 2 and is used to convert the liquid branching agent into the gaseous branching agent and input the gaseous branching agent into the Venturi tube 2.

[0103] The pressurization unit 1 is used to pressurize the gas and gaseous modifier inside the reaction unit and then deliver them to the reaction unit. In this embodiment, the pressurization unit 1 is preferably a gas booster pump, which provides the power to re-deliver the nitrogen mixed with the gaseous modifier into the reactor.

[0104] The reaction unit is used to heat and stir the gaseous modifier and reaction raw materials to carry out the long-chain branching modification reaction of rare earth cis-butadiene rubber.

[0105] It should be noted that the gas inside the reaction unit is a mixture of gases, which is mainly nitrogen and may also include small amounts of n-hexane, butadiene, disulfur dichloride gas, and a small amount of internal solvent.

[0106] Furthermore, the reaction unit and the feeding unit can respectively switch on and off the nitrogen source to provide a power source and facilitate the adjustment of their internal gas pressure.

[0107] The continuous production system of this application introduces different reaction raw materials into the reaction unit through multiple feeding units. The reaction unit continuously heats and stirs the reaction raw materials to induce polymerization, generating rare earth cis-butadiene rubber and a mixed gas. The liquid branching agent is converted into a gaseous branching agent through a conversion unit. The gaseous branching agent enters the Venturi tube 2 under pressure. The mixed gas in the reaction unit enters the input end of the pressurization unit 1 from the output end of the Venturi tube 2. At the same time, the mixed gas is pressurized by the pressurization unit 1. The gaseous branching agent follows the mixed gas and is sent into the reaction unit through the output end of the pressurization unit 1 under pressure. The long-chain branching modification of rare earth cis-butadiene rubber is achieved through continuous heating and stirring in the reaction unit. By continuously feeding the reaction raw materials through the feeding unit, continuously converting the liquid branching agent into a gaseous state through the conversion unit and sending it into the Venturi tube 2, continuously heating and stirring in the reaction unit, and continuously pressurizing through the pressurization unit 1, the long-chain branching modification reaction of rare earth cis-butadiene rubber is achieved in a continuous production process. The continuity of the chemical reaction ensures that the reaction conditions are constant and the product quality is stable during the long-chain branching modification of rare earth cis-butadiene rubber, thus realizing a continuous preparation process. This improves the production efficiency of long-chain branching modification of rare earth cis-butadiene rubber, reduces production costs, and significantly shortens the production cycle.

[0108] In some implementations, see Appendix Figure 2 As shown, the feeding unit includes a feeding tank 3, a second pipeline 4, a third pipeline 5, a first metering tank 7, a fourth pipeline 8, a second metering tank 9, a fifth pipeline 10, a sixth pipeline 11, a seventh pipeline 13, a metering pump 14, a first pressure regulating pipeline 15, a second pressure regulating pipeline 16, and a third pressure regulating pipeline 17.

[0109] The feed tank 3 has a first end and a second end that are arranged opposite each other along the height direction. Furthermore, a level gauge is installed in the feed tank 3 to monitor the level of the reaction raw materials in the feed tank 3.

[0110] One end of the second pipeline 4 is connected to the first end of the feed tank 3, and the other end of the second pipeline 4 is used to introduce reaction raw materials. A first valve 4a is installed on the second pipeline 4, and the first valve 4a is used to control the opening and closing of the second pipeline 4.

[0111] One end of the third pipeline 5 is connected to the second end of the feed tank 3, and the other end of the third pipeline 5 is connected to the first interface of the three-way valve 6. A second valve 5a is provided on the third pipeline 5, and the second valve 5a is used to control the opening and closing of the third pipeline 5.

[0112] The first metering tank 7 has a first end and a second end that are arranged opposite each other along the height direction.

[0113] One end of the fourth pipeline 8 is connected to the second interface of the three-way valve 6, and the other end of the fourth pipeline 8 is connected to the first end of the first metering tank 7.

[0114] The second metering tank 9 has a first end and a second end that are arranged opposite each other along the height direction.

[0115] One end of the fifth pipeline 10 is connected to the third port of the three-way valve 6, and the other end of the fifth pipeline 10 is connected to the first end of the second metering tank 9.

[0116] One end of the sixth pipe 11 is connected to the second end of the first metering tank 7, and the other end of the sixth pipe 11 is connected to the first interface of the four-way pipe 12.

[0117] One end of the seventh pipe 13 is connected to the second end of the second metering tank 9, and the other end of the seventh pipe 13 is connected to the second interface of the four-way pipe 12.

[0118] Metering pump 14 is connected to the third port of four-way pipe 12, and the fourth port of four-way pipe 12 is connected to the reaction unit.

[0119] One end of the first pressure regulating pipeline 15 is connected to the first end of the feed tank 3, and the other end of the first pressure regulating pipeline 15 is connected to the first interface of the tee pipe.

[0120] One end of the second pressure regulating pipeline 16 is connected to the first end of the first metering tank 7, and the other end of the second pressure regulating pipeline 16 is connected to the second interface of the tee pipe.

[0121] One end of the third pressure regulating pipeline 17 is connected to the first end of the second metering tank 9, and the other end of the third pressure regulating pipeline 17 is connected to the third interface of the tee pipe.

[0122] It should be further noted that pressure regulating valves are respectively installed on the first pressure regulating pipeline 15, the second pressure regulating pipeline 16 and the third pressure regulating pipeline 17.

[0123] Fine-tuning valves are installed on the first, second, and fourth interfaces of the third pipeline 5, the fourth pipeline 8, the fifth pipeline 10, the sixth pipeline 11, the seventh pipeline 13, and the four-way pipe 12, respectively, to control the on / off state of the pipelines and the flow rate of the reaction raw materials.

[0124] The working process of the feeding unit is described as follows: When the first valve 4a is opened, the reaction raw materials enter the feeding tank 3 through the second pipeline 4. Since nitrogen gas is introduced into the feeding tank 3, the gas pressure in the feeding tank 3, the first metering tank 7, and the second metering tank 9 are adjusted by the pressure regulating valve. The three-way valve 6 is adjusted so that the reaction raw materials enter the first metering tank 7 and the second metering tank 9 through the third pipeline 5, the fourth pipeline 8, and the fifth pipeline 10 under the action of gas pressure. Then, they enter the four-way pipe 12 through the sixth pipeline 11 and the seventh pipeline 13 respectively. The flow rate of the reaction raw materials is precisely controlled by the metering pump 14, and the reaction raw materials are sent into the reaction unit through the fourth port of the four-way pipe 12.

[0125] In conventional methods, only one metering tank is used. When a blockage or other malfunction occurs, the material cannot be fed, which will stop the production. In this application, by designing the pipeline connection between the first metering tank 7 and the second metering tank 9, a "one for backup" function is achieved, which ensures continuous and accurate production feeding of rare earth cis-butadiene rubber in long-chain branching modification.

[0126] In some embodiments, the feeding unit further includes a first support 18, a first level gauge 20, a second support 21, and a second level gauge 23.

[0127] The first support 18 is sleeved and connected to the side wall of the first metering tank 7, and the bottom of the first support 18 is provided with a first loss-in-weight scale 19.

[0128] The first level gauge 20 is installed at the first end of the first metering tank 7 and is located inside the first metering tank 7. The first level gauge 20 is used to monitor the level of the reaction raw materials inside the first metering tank 7.

[0129] The second support 21 is sleeved and connected to the side wall of the second metering tank 9, and the bottom of the second support 21 is provided with a second loss-in-weight scale 22.

[0130] The second level gauge 23 is installed at the first end of the second metering tank 9 and is located inside the second metering tank 9. The second level gauge 23 is used to monitor the level of the reaction raw materials inside the second metering tank 9.

[0131] Since the required flow rate of reactants during long-chain branching modification is relatively small, it is currently difficult to find suitable flow meters on the market. Therefore, the changes in the liquid level and weight of the reaction raw materials are monitored by using a first level gauge 20 in conjunction with a first loss-in-weight balance 19 and a second level gauge 23 in conjunction with a second loss-in-weight balance 22. The results are then converted into flow rates for flow control. It should be noted that both the first metering tank 7 and the second metering tank 9 are volume tubes, which facilitates the calculation of the flow rate of the reaction raw materials.

[0132] In some implementations, see Appendix Figure 1 As shown, the reaction unit includes a first reaction vessel 24, a first pipeline 25, multiple feed branches 26, a first drive device 27, a first double helix stirrer 28, a second reaction vessel 29, a first series pipeline 30, a second drive device 31, a second double helix stirrer 32, a third reaction vessel 33, a second series pipeline 36, a third drive device 37, and a third double helix stirrer 38.

[0133] The first reactor 24 has a first end and a second end that are arranged opposite each other along the height direction. The side wall of the first reactor 24 is provided with a first overflow port 24a. The first reactor 24 can heat the reaction raw materials inside it.

[0134] One end of the first pipeline 25 is connected to the second end of the first reactor 24.

[0135] One end of each of the multiple feed branches 26 is connected to the other end of the first pipeline 25; the other end of each of the multiple feed branches 26 is connected to a feed unit, specifically the fourth port of the four-way pipe 12 of the feed unit. The feed unit enters the first reactor 24 through the feed branches 26 and the first pipeline 25 to complete the reaction feeding.

[0136] In this embodiment, there are seven feeding units and seven corresponding feeding branches 26.

[0137] One end of the first series pipe 30 is connected to the first overflow port 24a, and the other end of the first series pipe 30 is connected to the second end of the second reactor 29. The reaction raw materials in the first reactor 24 enter the second reactor 29 through the first overflow port 24a and the first series pipe 30.

[0138] The first driving device 27 is located at the first end of the first reactor 24, and the first double-helix stirrer 28 is located inside the first reactor 24 and coaxially connected to the driving end of the first driving device 27. The first driving device 27 drives the first double-helix stirrer 28 to stir the reaction materials in the first reactor 24, and the polymerization reaction of the reaction materials is realized by heating and stirring.

[0139] The second reactor 29 has a first end and a second end arranged opposite to each other along the height direction. The side wall of the second reactor 29 is provided with a second overflow port 29a. The second reactor 29 can heat the reaction raw materials transported from the first reactor 24.

[0140] One end of the second series pipe 36 is connected to the second overflow port 29a, and the other end of the second series pipe 36 is connected to the second end of the third reactor 33. The reaction raw materials in the second reactor 29 enter the third reactor 33 through the second overflow port 29a and the second series pipe 36.

[0141] The second drive unit 31 is located at the first end of the second reactor 29, and the second double-helix stirrer 32 is located inside the second reactor 29 and coaxially connected to the drive end of the second drive unit 31. The second drive unit 31 drives the second double-helix stirrer 32 to stir the reaction materials in the second reactor 29, and further polymerization reaction of the reaction materials is achieved by heating and stirring.

[0142] The third reactor 33 has a first end and a second end that are arranged opposite each other along the height direction. The side wall of the third reactor 33 is provided with a third overflow port 33a. The third overflow port 33a and the storage tank are connected through a discharge pipe 34. The first end of the third reactor 33 and the input end of the Venturi tube 2 are connected through a first bend pipe 35. The first end of the third reactor 33 and the output end of the pressurization unit 1 are connected through a second bend pipe 46. A fifth control valve 461 is provided on the second bend pipe 46.

[0143] The third reactor 33 heats the reaction raw materials transported from the second reactor 29 and produces rare earth cis-butadiene rubber and mixed gas. The mixed gas enters the input end of the pressurization unit 1 through the first bend pipe 35 and the input end of the venturi tube 2. The pressurization unit 1 pressurizes the mixed gas. The gaseous branching agent in the venturi tube 2 follows the mixed gas and is sent into the reaction unit through the output end of the pressurization unit 1 under the action of gas pressure. Through continuous heating and stirring in the reaction unit, the rare earth cis-butadiene rubber is modified into long-chain branching. Finally, the material is collected by entering the storage tank through the third overflow port 33a and the discharge pipe 34.

[0144] The third driving device 37 is located at the first end of the third reaction vessel 33, and the third double helix stirrer 38 is located inside the third reaction vessel 33 and coaxially connected to the driving end of the third driving device 37. The third driving device 37 drives the third double helix stirrer 38 to heat and stir the rare earth cis-butadiene rubber and gaseous branching agent in the third reaction vessel 33 to achieve long-chain branching modification of rare earth cis-butadiene rubber.

[0145] In this embodiment, the first driving device 27, the second driving device 31, and the third driving device 37 are all rotary motors. Level gauges are installed in the first reaction vessel 24, the second reaction vessel 29, and the third reaction vessel 33 to monitor the liquid level of the material inside. The first reaction vessel 24, the second reaction vessel 29, and the third reaction vessel 33 can all switch on and off the nitrogen gas source to provide a power source and regulate the gas pressure inside the vessel.

[0146] The working process of the reaction unit is as follows: The reactants enter the first reactor 24 through the first pipeline 25 and the feed branch 26. The first reactor 24 stirs and heats the reactants to induce polymerization. Then, the reactants enter the second reactor 29 through the first overflow port 24a and the first series pipeline 30. The second reactor 29 further stirs and heats the reactants to induce further polymerization. Then, the reactants enter the third reactor 33 through the second overflow port 29a and the second series pipeline 36. The third reactor 33 stirs and heats the reactants. The mixture is heated and mixed to produce rare earth butadiene rubber and mixed gas. The mixed gas enters the input end of the pressurization unit 1 through the first bend pipe 35 and the input end of the venturi tube 2. The pressurization unit 1 pressurizes the mixed gas. The gaseous branching agent in the venturi tube 2 follows the mixed gas and is sent to the third reactor 33 through the second bend pipe 46 through the output end of the pressurization unit 1 under the action of gas pressure. The rare earth butadiene rubber is modified into long chain branching by continuous heating and stirring in the third reactor 33. Finally, the material is collected by entering the storage tank through the third overflow port 33a and the discharge pipe 34.

[0147] By continuously heating and stirring the raw materials in multiple reactors (first reactor 24, second reactor 29 and third reactor 33), the raw materials undergo a continuous polymerization reaction, which improves the purity of rare earth cis-butadiene rubber and makes the long-chain branching modification reaction more complete, thus ensuring product quality and yield.

[0148] In some implementations, see Appendix Figure 1 As shown, the first bend 35 and the venturi tube 2 are connected through a buffer unit, which includes a buffer tank 40.

[0149] The buffer tank 40 has an inlet pipe 41 and an outlet pipe 42 inside. The buffer tank 40 contains a buffer solution. The inlet pipe 41 is located on the outside of the buffer tank 40 and is connected to the first bend pipe 35. The inlet pipe 41 is located on the inside of the buffer tank 40 and is below the surface of the buffer solution. The outlet pipe 42 is connected to the buffer tank 40 and is located above the surface of the buffer solution. It is preferably located near the inner top wall of the buffer tank 40. The other end of the outlet pipe 42 is connected to the input end of the venturi tube 2. The buffer unit based on the buffer tank 40 is placed between the venturi tube 2 and the third reactor 33. It can buffer the air intake at the input end of the venturi tube 2, prevent the pressure of the mixed gas inside the third reactor 33 from being too high and damaging the pressurization unit 1, and ensure the normal operation of the gas circulation device.

[0150] Furthermore, the buffer tank 40 is provided with a first discharge port 43 at the bottom, and a first valve 4a is installed on the first discharge port 43 to discharge the buffer solution from the buffer tank 40, facilitating subsequent replacement of the buffer solution. A first control valve 411 is installed on the inlet pipe 41 to control the mixed gas to enter the buffer tank 40 directly from the third reactor 33; a sixth control valve 421 is installed on the exhaust pipe 42 to control the mixed gas entering the buffer tank 40 to be drawn into the venturi tube 2 by the pressurization unit 1 and mixed with the gaseous modifier entering the venturi tube 2.

[0151] In some embodiments, the buffer unit further includes a protection module, which includes a protection branch pipe 44, a back pressure valve 441, a second control valve 442, a first fine-tuning valve 443, a third control valve 412, and a drain pipe 45.

[0152] The protective branch pipe 44 is connected to the inlet pipes 41 on both sides of the first control valve 411, allowing the mixed gas discharged from the third reactor 33 to enter the buffer tank 40 through the first control valve 411 or through the protective branch pipe 44 and then through the inlet pipe 41 behind the first control valve 411. A back pressure valve 441 is installed on the protective branch pipe 44. By setting the set pressure of the back pressure valve 441, the gas pressure passing through the protective branch pipe 44 can be controlled to provide overpressure protection for the reactor. A second control valve 442 is installed on the protective branch pipe 44 on the input side of the back pressure valve 441, used to control the opening and closing of the protective branch pipe 44. A first fine-tuning valve 443 is installed on the protective branch pipe 44 on the output side of the back pressure valve 441, used to cut off or adjust the gas flow rate in the protective branch pipe 44. The first fine-tuning valve 443 can preferably be a needle valve. The third control valve 412 is installed on the inlet pipe 41 behind the protective branch pipe 44 along the gas flow direction. It is used to control whether the buffer tank 40 receives the mixed gas from the third reactor 33 delivered through the first control valve 411 or the protective branch pipe 44. The vent pipe 45 is installed on the buffer tank 40, and a fourth control valve 451 is installed on the vent pipe 45. The vent pipe 45 can be opened or closed by the fourth control valve 451. When the sixth control valve 421 is closed, the mixed gas entering the buffer tank 40 can be discharged through the vent pipe 45.

[0153] In this embodiment, when it is necessary to add the modifier into the reactor, the first control valve 411, the third control valve 412, the sixth control valve 421 and the fifth control valve 461 are opened, the fourth control valve 451 is closed, and the pressurization unit 1 is started. The mixed gas in the third reactor 33 enters the buffer tank 40 through the first bend pipe 35 and the inlet pipe 41. The mixed gas then enters the Venturi tube 2 from the buffer tank 40 through the exhaust pipe 42. In the Venturi tube 2, the mixed gas mixes with the gaseous modifier. After being pressurized by the pressurization unit 1, it is then transported to the third reactor 33 through the second bend pipe 46.

[0154] It should be noted that during the above process, the second control valve 442 and the first fine-tuning valve 443 are in the open state. When the gas pressure in the third reactor 33 is higher than the set pressure of the back pressure valve 441, the mixed gas will be transported not only through the first control valve 411 but also through the protective branch pipe 44. When no modifier needs to be added to the third reactor 33, the first control valve 411, the sixth control valve 421, and the fifth control valve 461 are closed, and the fourth control valve 451 is opened. When the gas pressure in the third reactor 33 is higher than the set pressure of the back pressure valve 441, the mixed gas enters the protective branch pipe 44 through the first bend pipe 35, and then enters the buffer tank 40 through the inlet pipe 41. The mixed gas is then discharged through the vent pipe 45, thereby achieving automatic pressure reduction in the third reactor 33 under overpressure conditions and effectively protecting the third reactor 33 from damage.

[0155] In some implementations, see Appendix Figure 3 and 4 As shown, the conversion unit includes a feeding tank 50, a heating vessel 51, an eighth pipeline 52, a first regulating valve 521, a fourth pressure regulating pipeline 53, and a second regulating valve 531.

[0156] The feeding tank 50 has a top and a bottom that are arranged opposite each other along the height direction. The top of the feeding tank 50 is provided with a feed port 100 for feeding liquid branching agent and an air inlet 200 for connecting to a nitrogen source.

[0157] Among them, the liquid branching agent can be dichlorodisulfur, also known as sulfur monochloride, which is an inorganic compound with the chemical formula S2Cl2, and is a yellow to slightly red liquid.

[0158] The nitrogen source is used to supply nitrogen to the feeding tank 50, which is used to pressurize and boost the internal pressure of the feeding tank 50, and the branching agent in the feeding tank 50 is sent into the heating vessel 51 by the action of air pressure.

[0159] It should be noted that a capacitive level gauge is also installed in the feeding tank 50 to measure the liquid level of the branching agent in the feeding tank 50.

[0160] The heating vessel 51 has a top and a bottom that are arranged opposite each other along the height direction. The heating vessel 51 is located below the feeding tank 50 and is used to heat the liquid branching agent into a gaseous product. That is, the dichlorodisulfide branching agent is converted from a liquid state to a gaseous state by heating in the heating vessel 51.

[0161] It should be noted that the boiling point of dichlorodisulfur is about 138°C. In this embodiment, the heating temperature of the heating vessel 51 needs to reach 138°C or higher in order to vaporize the liquid dichlorodisulfur.

[0162] The bottom of the feeding tank 50 and the top of the heating vessel 51 are connected by an eighth pipe 52, on which a first regulating valve 521 is provided. In this embodiment, the first regulating valve 521 is preferably a fine-tuning valve. The requirement of the fine-tuning valve is that the valve opening gradually increases, and it can be continuously and finely adjusted from closed to the maximum opening, which ensures the stability and controllability of the branching agent flow.

[0163] The flow rate of the branching agent entering the heating vessel 51 from the eighth pipe 52 is precisely adjusted by a fine-tuning valve, so that the branching agent in the eighth pipe 52 enters the heating vessel 51 under controllable flow conditions.

[0164] The top of the feeding tank 50 and the top of the heating vessel 51 are connected via a fourth pressure regulating pipe 53. Specifically, the top of the feeding tank 50 has an equalization port 300. One end of the fourth pressure regulating pipe 53 is connected to the equalization port 300, and the other end is connected to the top of the heating vessel 51. A second regulating valve 531 is installed on the fourth pressure regulating pipe 53. In this embodiment, the second regulating valve 531 is preferably a needle valve. The valve core of the needle valve is designed as a very sharp cone that inserts into the valve seat like a needle. This design allows the needle valve to withstand higher pressures and has good sealing performance. Therefore, the needle valve is particularly suitable for sealing applications requiring small flow rates and high pressures of gas or liquid media.

[0165] Based on this, the gas flow rate in the feeding tank 50 and the heating vessel 51 is precisely adjusted by the needle valve, so that the gas pressure in the feeding tank 50 is greater than the gas pressure in the heating vessel 51, so that the branching agent in the feeding tank 50 can smoothly enter the heating vessel 51 through the eighth pipeline 52 under the action of the gas pressure difference. The heating vessel 51 converts the branching agent from liquid to gas by heating.

[0166] The top of the heating vessel 51 is connected to one end of the ninth pipe 54, and the other end of the ninth pipe 54 is connected to the venturi tube 2.

[0167] Nitrogen gas is injected into the feeding tank 50 through a nitrogen source. With the connection of the fourth pressure regulating pipeline 53, the gas pressure in the feeding tank 50 and the heating vessel 51 is equalized. The gas flow rate is adjusted by the second regulating valve 531, allowing the liquid branching agent to enter the eighth pipeline 52 under the influence of the pressure difference. The flow rate of the liquid branching agent in the eighth pipeline 52 is adjusted by the first regulating valve 521, allowing the liquid branching agent to enter the heating vessel 51 for heating, thus converting the branching agent from liquid to gas. By controlling the flow rates of the liquid and gaseous states, the liquid-to-gas conversion rate is controlled, enabling the gaseous branching agent to be introduced into the Venturi tube 2 via the ninth pipeline 54.

[0168] In some embodiments, a second on / off valve 541 is also provided on the eighth pipeline 52, located between the first regulating valve 521 and the bottom of the feed tank 50.

[0169] By controlling the opening and closing of the eighth pipeline 52 through the second on / off valve 541, the eighth pipeline 52 connecting the feeding tank 50 and the heating vessel 51 can be quickly cut off or connected, meeting the needs of rapid response.

[0170] In some embodiments, a discharge valve 55 is provided at the bottom of the heating vessel 51; a vent 400 for feeding cleaning fluid is also provided at the top of the feeding tank 50; the conversion unit also includes a first discharge pipe 56; the discharge valve 55 has a discharge port 551; one end of the first discharge pipe 56 is connected to the discharge port 551; the other end of the first discharge pipe 56 is connected to the first collection tank; and a first on / off valve 561 is provided on the first discharge pipe 56.

[0171] After the branching modification of rare earth butadiene rubber is completed, and the branching agent is converted from liquid to gas in the heating kettle 51, some liquid branching agent will remain in the heating kettle 51 under normal circumstances. Cleaning liquid is added to the feeding tank 50 through the vent 400. The gas pressure is adjusted by the second regulating valve 531 so that the cleaning liquid enters the eighth pipeline 52 to clean the inside of the heating kettle 51. The cleaning liquid and the liquid branching agent form a mixture. The discharge valve 55 is opened, and the mixture enters the first discharge pipeline 56 through the discharge port 551. The first on / off valve 561 controls the opening and closing of the first discharge pipeline 56 so that the mixture can enter the first collection tank through the first discharge pipeline 56 for collection, thereby realizing the liquid cleaning of the heating kettle 51.

[0172] Furthermore, the conversion unit also includes a second discharge line 57, a third discharge line 58, a third on / off valve 571, a fourth on / off valve 572, and a fifth on / off valve 581.

[0173] One end of the second discharge pipe 57 is connected to the top of the heating vessel 51, and the other end of the second discharge pipe 57 is connected to the second collection tank (not shown in the figure). The second discharge pipe 57 is equipped with a third on / off valve 571 near the top of the heating vessel 51 and a fourth on / off valve 572 near the second collection tank.

[0174] One end of the third discharge pipe 58 is connected to the second discharge pipe 57 between the third shut-off valve 571 and the fourth shut-off valve 572; the other end of the third discharge pipe 58 is connected to the first discharge pipe 56 between the first shut-off valve 561 and the discharge port 551; a fifth shut-off valve 581 is provided on the third discharge pipe 58.

[0175] Following the previous text, after the branching agent is converted from liquid to gas in the heating vessel 51, not only some liquid branching agent remains, but also some gaseous branching agent remains in the heating vessel 51. Nitrogen gas is introduced into the feeding tank 50 through the air inlet 200. At this time, the first regulating valve 521, the second on-off valve 541, the second regulating valve 531 are opened, the fourth on-off valve 572, the fifth on-off valve 581 are opened, and the third on-off valve 571 is closed. Nitrogen gas enters the heating vessel 51 through the eighth pipeline 52 to perform air blowing cleaning of the interior of the heating vessel 51. Nitrogen gas and gaseous branching agent form a mixed gas. The discharge valve 55 is opened, and the mixed gas flows through the discharge port 551 through the first discharge pipeline 56, the third discharge pipeline 58, and the second discharge pipeline 57 into the second collection tank for collection, thereby realizing the gaseous cleaning of the heating vessel 51.

[0176] Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention. Those skilled in the art can make changes, modifications, substitutions and variations to the above embodiments within the scope of the invention without departing from the principles and spirit of the invention, and all such changes should fall within the protection scope of the claims of the present invention.

Claims

1. A continuous production system, characterized in that, The application relates to a reaction system for preparing branched oil, which comprises: a reaction unit; a plurality of feeding units respectively in communication with the reaction unit, each of the feeding units being used for feeding different reaction raw materials into the reaction unit, the reaction raw materials including solvent oil, monomers and catalysts; a booster unit (1) having an input end and an output end, the output end of the booster unit (1) being in communication with the reaction unit; a Venturi tube (2) having an input end and an output end, the input end of the Venturi tube (2) being in communication with the reaction unit, and the output end of the Venturi tube (2) being in communication with the input end of the booster unit (1); a conversion unit in communication with the Venturi tube (2) and used for converting liquid branched agents into gaseous branched agents and feeding the gaseous branched agents into the Venturi tube (2); the booster unit (1) is used for boosting the gas in the reaction unit and gaseous modifying agents and feeding the boosted gas into the reaction unit; the reaction unit is used for heating and stirring the gaseous modifying agents and the reaction raw materials. The feeding unit comprises: a feeding tank (3) having a first end and a second end arranged oppositely along the height direction; 2. The continuous production system of claim 1, wherein, a second pipeline (4), one end of the second pipeline (4) being in communication with the first end of the feeding tank (3), and the other end of the second pipeline (4) being used for feeding the reaction raw materials; a first valve (4a) is arranged on the second pipeline (4); a third pipeline (5), one end of the third pipeline (5) being in communication with the second end of the feeding tank (3), and the other end of the third pipeline (5) being in communication with a first interface of a three-way valve (6); a second valve (5a) is arranged on the third pipeline (5); a first metering tank (7) having a first end and a second end arranged oppositely along the height direction; a fourth pipeline (8), one end of the fourth pipeline (8) being in communication with a second interface of the three-way valve (6), and the other end of the fourth pipeline (8) being in communication with the first end of the first metering tank (7); a second metering tank (9) having a first end and a second end arranged oppositely along the height direction; a fifth pipeline (10), one end of the fifth pipeline (10) being in communication with a third interface of the three-way valve (6), and the other end of the fifth pipeline (10) being in communication with the first end of the second metering tank (9); a sixth pipeline (11), one end of the sixth pipeline (11) being in communication with the second end of the first metering tank (7), and the other end of the sixth pipeline (11) being in communication with a first interface of a four-way tube (12); a seventh pipeline (13), one end of the seventh pipeline (13) being in communication with the second end of the second metering tank (9), and the other end of the seventh pipeline (13) being in communication with a second interface of the four-way tube (12); a metering pump (14) in communication with a third interface of the four-way tube (12), and a fourth interface of the four-way tube (12) being in communication with the reaction unit; a first pressure regulating pipeline (15), one end of the first pressure regulating pipeline (15) being in communication with the first end of the feeding tank (3), and the other end of the first pressure regulating pipeline (15) being in communication with a first interface of a three-way tube. ​ ​ A second pressure regulating pipeline (16) has one end in communication with the first end of the first metering tank (7) and the other end in communication with the second interface of the three-way pipe. A third pressure regulating pipeline (17) has one end in communication with the first end of the second metering tank (9) and the other end in communication with the third interface of the three-way pipe.

3. The continuous production system of claim 2, wherein, The feeding unit further comprises: A first support (18) is sleeved and connected to the side wall of the first metering tank (7), and the bottom of the first support (18) is provided with a first loss-in-weight scale (19). A first liquid level meter (20) is arranged at the first end of the first metering tank (7) and located inside the first metering tank (7). A second support (21) is sleeved and connected to the side wall of the second metering tank (9), and the bottom of the second support (21) is provided with a second loss-in-weight scale (22). A second liquid level meter (23) is arranged at the first end of the second metering tank (9) and located inside the second metering tank (9).

4. The continuous production system of claim 3, wherein, The reaction unit comprises: A first reaction kettle (24) has a first end and a second end arranged opposite in the height direction, and the side wall of the first reaction kettle (24) is provided with a first overflow port (24a). A first pipeline (25) has one end in communication with the second end of the first reaction kettle (24). A plurality of feeding branches (26) have one end in communication with the other end of the first pipeline (25) respectively. A first driving device (27) is arranged at the first end of the first reaction kettle (24). A first double helix stirrer (28) is located inside the first reaction kettle (24) and coaxially connected with the driving end of the first driving device (27). A second reaction kettle (29) has a first end and a second end arranged opposite in the height direction, and the side wall of the second reaction kettle (29) is provided with a second overflow port (29a). A first series pipeline (30) has one end in communication with the first overflow port (24a) and the other end in communication with the second end of the second reaction kettle (29). A second driving device (31) is arranged at the first end of the second reaction kettle (29). A second double helix stirrer (32) is located inside the second reaction kettle (29) and coaxially connected with the driving end of the second driving device (31). The third reactor (33) has a first end and a second end arranged opposite in the height direction, a third overflow port (33a) is arranged on the side wall of the third reactor (33), the third overflow port (33a) and the storage tank are communicated through a discharge pipe (34), the first end of the third reactor (33) and the venturi tube (2) are communicated through a first elbow pipe (35), the first end of the third reactor (33) and the output end of the booster unit (1) are communicated through a second elbow pipe (46), and a fifth control valve (461) is arranged on the second elbow pipe (46); A second series pipeline (36) is communicated with the second overflow port (29a) at one end and communicated with the second end of the third reactor (33) at the other end; A third driving device (37) is arranged at the first end of the third reactor (33); and A third double helix stirrer (38) is arranged inside the third reactor (33) and coaxially connected with the driving end of the third driving device (37).

5. The continuous production system of claim 4, wherein, The first elbow pipe (35) and the venturi tube (2) are communicated through a buffer unit, and the buffer unit comprises: A buffer tank (40) has a gas inlet pipe (41) and a gas outlet pipe (42) arranged inside, a buffer solution is arranged in the buffer tank (40), the gas inlet pipe (41) is connected with the first elbow pipe (35) at one end outside the buffer tank (40), the gas inlet pipe (41) is arranged below the liquid level of the buffer solution at one end inside the buffer tank (40), the gas outlet pipe (42) is arranged above the liquid level of the buffer solution at one end connected with the buffer tank (40), and the other end of the gas outlet pipe (42) is connected with the input end of the venturi tube (2); and / or A first discharge port (43) is arranged at the bottom of the buffer tank (40), and a first valve is arranged on the first discharge port (43); and / or A first control valve (411) is arranged on the gas inlet pipe (41); A sixth control valve (421) is arranged on the gas outlet pipe (42).

6. The continuous production system of claim 5, wherein, The buffer unit further comprises a protection module, and the protection module comprises: A protection branch pipe (44) is communicated with the gas inlet pipe (41) on both sides of the first control valve (411); A back pressure valve (441) is arranged on the protection branch pipe (44); A second control valve (442) is arranged on the protection branch pipe (44) on one side of the input end of the back pressure valve (441); A first fine adjustment valve (443) is arranged on the protection branch pipe (44) on one side of the output end of the back pressure valve (441); A third control valve (412) is arranged on the gas inlet pipe (41) downstream of the protection branch pipe (44) in the gas flow direction; and An emptying pipe (45) is arranged on the buffer tank (40), and a fourth control valve (451) is arranged on the emptying pipe (45).

7. The continuous production system of claim 3, wherein, The conversion unit comprises: a charging tank (50) having a top portion and a bottom portion arranged oppositely along a height direction; the top portion of the charging tank (50) is provided with a feeding port (100) for feeding liquid branching agent and a gas inlet (200) for communicating with a nitrogen source; and a heating kettle (51) having a top portion and a bottom portion arranged oppositely along the height direction; the heating kettle (51) is located below the charging tank (50) and is used for converting the liquid branching agent into gaseous branching agent; the bottom portion of the charging tank (50) and the top portion of the heating kettle (51) are communicated through an eighth pipeline (52), and the eighth pipeline (52) is provided with a first regulating valve (521); the top portion of the charging tank (50) and the top portion of the heating kettle (51) are communicated through a fourth pressure regulating pipeline (53), and the fourth pressure regulating pipeline (53) is provided with a second regulating valve (531); the top portion of the heating kettle (51) and one end of a ninth pipeline (54) are communicated, and the other end of the ninth pipeline (54) and a Venturi tube (2) are communicated.

8. The continuous production system of claim 7, wherein, The eighth pipeline (52) is further provided with a second on-off valve (541) located between the first regulating valve (521) and the bottom portion of the charging tank (50).

9. The continuous production system of claim 7, wherein, The bottom portion of the heating kettle (51) is provided with a discharge valve (55); the conversion unit further comprises a first discharge pipeline (56), the discharge valve (55) has a discharge port (551), one end of the first discharge pipeline (56) and the discharge port (551) are communicated, the other end of the first discharge pipeline (56) and a first collection tank are communicated, and the first discharge pipeline (56) is provided with a first on-off valve (561).

10. The continuous production system of claim 9, wherein, The conversion unit further comprises: a second discharge pipeline (57), one end of the second discharge pipeline (57) and the top portion of the heating kettle (51) are communicated, and the other end of the second discharge pipeline (57) and a second collection tank are communicated; the second discharge pipeline (57) is provided with a third on-off valve (571) close to the top portion of the heating kettle (51) and a fourth on-off valve (572) close to the second collection tank; and a third discharge pipeline (58), one end of the third discharge pipeline (58) and the second discharge pipeline (57) between the third on-off valve (571) and the fourth on-off valve (572) are communicated, and the other end of the third discharge pipeline (58) and the first discharge pipeline (56) between the first on-off valve (561) and the discharge port (551) are communicated; the third discharge pipeline (58) is provided with a fifth on-off valve (581).

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