A continuous hydrogenation reaction system, method and related applications of sulfolene

Abstract

The present invention provides a continuous hydrogenation reaction system, method and related applications for sulfolene. The continuous hydrogenation reaction system for sulfolene includes a circulation pump, an auxiliary reactor, a main reactor, an external circulation cooler and a reaction circulation tank. The hydrogen remaining after the second hydrogenation reaction enters the reaction circulation tank for storage, and the main reactor draws hydrogen from the reaction circulation tank, realizing the hydrogenation reaction of sulfolene, reducing the circulating hydrogen compressor link, greatly improving the hydrogenation reaction efficiency and reducing the production cost; after the first hydrogenation reaction of sulfolene, hydrogen and catalyst occurs in the auxiliary reactor, and the second hydrogenation reaction is carried out in the main reactor, and the conversion rate of sulfolene is maintained at a relatively high level, reducing the generation of by-products; the hydrogen, catalyst and sulfolene are pumped into the main reactor through the circulation pump, and the liquid-phase product input from the reaction circulation tank is pumped into the main reactor, realizing the continuous production of the hydrogenation reaction of sulfolene and improving the production efficiency.

Description

Technical Field

[0001] The present invention relates to the technical field of sulfolane preparation, and particularly relates to a continuous hydrogenation reaction system and method for cyclobutene sulfone, an application of the continuous hydrogenation reaction system for cyclobutene sulfone in the preparation of sulfolane, and an application of the continuous hydrogenation reaction method for cyclobutene sulfone in the preparation of sulfolane. Background Art

[0002] Sulfolane is a commonly used solvent and belongs to small specialty fine chemical products. Most of the sulfolane is produced by the hydrogenation reaction of cyclobutene sulfone. At present, the hydrogenation reaction of cyclobutene sulfone mostly adopts the batch kettle process. Summary of the Invention

[0003] The existing hydrogenation reaction system for cyclobutene sulfone has the following problems: the hydrogenation reaction is intermittent, and the remaining hydrogen after the reaction cannot be completely recovered, resulting in a large loss of hydrogen and increasing the production cost. In view of the above problems, it is necessary to propose a continuous hydrogenation reaction system for cyclobutene sulfone to solve or partially solve the above problems. The technical solutions proposed by the present invention are as follows:

[0004] In a first aspect, the present invention proposes a continuous hydrogenation reaction system for cyclobutene sulfone, including a circulation pump, an auxiliary reactor, an external circulation cooler, a main reactor, and a reaction circulation tank, wherein:

[0005] The circulation pump has an input end connected to the reaction circulation tank and an output end connected to the auxiliary reactor. A hydrogen inlet, a cyclobutene sulfone inlet, and a catalyst inlet are provided between the circulation pump and the auxiliary reactor, and are used to pump a first mixture of hydrogen, the liquid phase product transported from the reaction circulation tank, the catalyst, and cyclobutene sulfone into the auxiliary reactor;

[0006] The auxiliary reactor is connected to the circulation pump and the external circulation cooler at both ends, and is used to perform a first hydrogenation reaction on the first mixture and hydrogen, and transport the obtained second mixture and unreacted hydrogen to the external circulation cooler;

[0007] The external circulation cooler has an inlet end connected to the auxiliary reactor and an outlet end connected to the main reactor, and is used to cool the second mixture and unreacted hydrogen input from the auxiliary reactor and transport them to the main reactor;

[0008] The main reactor is connected to the reaction circulation tank, and is used to draw hydrogen from the reaction circulation tank, and transport the liquid phase product and unreacted hydrogen obtained by performing a second hydrogenation reaction on the input hydrogen, the second mixture, and the drawn hydrogen to the reaction circulation tank;

[0009] The reaction circulation tank is respectively connected to the main reactor and the circulation pump, and is used for transporting the liquid-phase product input by the main reactor to the circulation pump and / or discharging it, and supplying the unreacted hydrogen to the main reactor.

[0010] Furthermore, the main reactor is a Venturi vacuum generator. The main reactor includes a feed inlet, an adsorption port, a nozzle and a discharge port. The feed inlet is connected to the outlet end of the external circulation cooler for receiving the second mixture and the unreacted hydrogen; the nozzle is connected to the circulation pump for injecting the second mixture input by the circulation pump so as to generate negative pressure at the adsorption port; the adsorption port is connected to the reaction circulation tank for sucking hydrogen from the reaction circulation tank; the discharge port is connected to the reaction circulation tank for transporting the liquid-phase product obtained from the second hydrogenation reaction to the reaction circulation tank.

[0011] Furthermore, it further includes a hydrogen regulating valve and a pressure sensor arranged on the reaction circulation tank. The pressure sensor is connected to the hydrogen regulating valve, and the hydrogen regulating valve is connected to the hydrogen inlet to adjust its own valve opening according to the pressure of the pressure sensor.

[0012] Furthermore, the external circulation cooler is provided with a first cooling medium inlet and a first cooling medium outlet.

[0013] Furthermore, a cooling coil is arranged inside the reaction circulation tank, and the inlet and outlet of the cooling coil are used for transporting the second cooling medium.

[0014] Furthermore, a liquid-phase product outlet is arranged between the reaction circulation tank and the circulation pump, and the liquid-phase product outlet is used for outputting the liquid-phase product.

[0015] In a second aspect, the present invention also proposes an application of the continuous hydrogenation reaction system of sulfolene in the preparation of sulfolane.

[0016] In a third aspect, the present invention also proposes a continuous hydrogenation reaction method of sulfolene, including:

[0017] Pumping the first mixture obtained by mixing hydrogen, the liquid-phase product transported by the reaction circulation tank, a catalyst and sulfolene by a circulation pump into the auxiliary reactor;

[0018] Performing a first hydrogenation reaction on the first mixture and hydrogen by the auxiliary reactor, and transporting the obtained second mixture and the unreacted hydrogen to the external circulation cooler;

[0019] Cooling the second mixture and the unreacted hydrogen input by the auxiliary reactor by the external circulation cooler and transporting them to the main reactor;

[0020] The main reactor draws hydrogen from the reaction circulation tank, and conveys the input hydrogen, the second mixture, the liquid-phase product obtained from the second hydrogenation reaction, and the unreacted hydrogen to the reaction circulation tank;

[0021] The reaction circulation tank conveys the liquid-phase product input from the main reactor to the circulation pump and / or discharges it, and supplies the unreacted hydrogen to the main reactor.

[0022] Fourthly, the present invention also proposes an application of the continuous hydrogenation reaction method of sulfolene in the preparation of sulfolane.

[0023] Based on the above technical solutions, the beneficial effects of the present invention compared with the prior art are as follows:

[0024] The present invention provides a continuous hydrogenation reaction system for sulfolene, including a circulation pump, an auxiliary reactor, an external circulation cooler, a main reactor, and a reaction circulation tank. The hydrogen remaining after the second hydrogenation reaction enters the reaction circulation tank for storage. The main reactor draws hydrogen from the reaction circulation tank, realizing the recovery of hydrogen, reducing the loss of hydrogen, and lowering the production cost; sulfolene and hydrogen first undergo the first hydrogenation reaction in the auxiliary reactor under the action of a catalyst, and then continue the second hydrogenation reaction in the main reactor. The conversion rate of sulfolene can be maintained at a relatively high level, and more products are obtained from the hydrogenation reaction, enabling greater utilization of hydrogen and thus reducing the loss of hydrogen; the hydrogen, catalyst, and sulfolene are pumped into the main reactor through the circulation pump, and the liquid-phase product conveyed from the reaction circulation tank is also pumped into the main reactor, realizing the continuous production of the hydrogenation reaction of sulfolene and improving the production efficiency. Description of the Drawings

[0025] Figure 1 is a schematic structural diagram of the continuous hydrogenation reaction system for sulfolene in Embodiment 1 of the present invention;

[0026] Figure 2 is a schematic structural diagram of the main reactor in Embodiment 1 of the present invention;

[0027] Figure 3 is a schematic flow diagram of the continuous hydrogenation reaction method of sulfolene in Embodiment 2 of the present invention.

[0028] Among them, 1 - auxiliary reactor; 2 - external circulation cooler; 3 - main reactor; 31 - feed inlet; 32 - adsorption port; 33 - nozzle; 34 - discharge port; 4 - reaction circulation tank; 5 - circulation pump; 6 - hydrogen regulating valve. Detailed Embodiments

[0029] To make the objectives, technical solutions and advantages of the present invention clearer and more understandable, the present invention will be further described in detail below in conjunction with the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not used to limit the present invention.

[0030] Embodiment 1

[0031] An embodiment of the present invention provides a continuous hydrogenation reaction system for sulfolene, as Figure 1 shown, which includes a circulation pump 5, an auxiliary reactor 1, an external circulation cooler 2, a main reactor 3, and a reaction circulation tank 4, wherein:

[0032] The circulation pump 5 has an input end connected to the reaction circulation tank 4 and an output end connected to the auxiliary reactor 1. A hydrogen inlet, a sulfolene inlet, and a catalyst inlet are provided between the circulation pump 5 and the auxiliary reactor 1, and are used to pump a first mixture obtained by mixing hydrogen, the liquid-phase product transported from the reaction circulation tank 4, the catalyst, and sulfolene into the auxiliary reactor 1.

[0033] The auxiliary reactor 1 is connected to the circulation pump 5 and the external circulation cooler 2 at both ends respectively, and is used to perform a first hydrogenation reaction on the first mixture and hydrogen, and transport the obtained second mixture and unreacted hydrogen to the external circulation cooler 2.

[0034] The external circulation cooler 2 has an inlet end connected to the auxiliary reactor 1 and an outlet end connected to the main reactor 3, and is used to cool the second mixture and unreacted hydrogen input from the auxiliary reactor 1 and transport them to the main reactor 3.

[0035] Specifically, a first hydrogenation reaction occurs in the auxiliary reactor 1. Since the hydrogenation reaction is exothermic, the external circulation cooler 2 is required to cool the second mixture and unreacted hydrogen input from the auxiliary reactor 1 to reach the optimal temperature for the second hydrogenation reaction, so as to ensure that the second hydrogenation reaction is more complete, make greater use of hydrogen, and thus reduce the loss of hydrogen.

[0036] The main reactor 3 is connected to the reaction circulation tank 4, and is used to draw hydrogen from the reaction circulation tank 4, and transport the hydrogen, the second mixture, the liquid-phase product obtained by performing a second hydrogenation reaction on the drawn hydrogen, and unreacted hydrogen to the reaction circulation tank 4;

[0037] The reaction circulation tank 4 is connected to the main reactor 3 and the circulation pump 5 respectively, and is used to transport the liquid-phase product input from the main reactor 3 to the circulation pump 5 and / or discharge it, and supply unreacted hydrogen to the main reactor 3.

[0038] The continuous hydrogenation reaction system of sulfolene proposed by the present invention includes a circulation pump 5, an auxiliary reactor 1, an external circulation cooler 2, a main reactor 3 and a reaction circulation tank 4. The hydrogen remaining after the second hydrogenation reaction enters the reaction circulation tank 4 for storage. The main reactor 3 draws hydrogen from the reaction circulation tank 4, realizing the recovery of hydrogen, reducing the loss of hydrogen, and lowering the production cost. Sulfolene and hydrogen first undergo the first hydrogenation reaction in the auxiliary reactor 1 under the action of a catalyst, and then continue the second hydrogenation reaction in the main reactor 3. The conversion rate of sulfolene can be maintained at a relatively high level, and more products are obtained from the hydrogenation reaction, which can utilize hydrogen to a greater extent, thereby reducing the loss of hydrogen. The hydrogen, catalyst and sulfolene are pumped into the main reactor 3 by the circulation pump 5, and the liquid-phase product transported from the reaction circulation tank 4 is also pumped into the main reactor 3, realizing the continuous production of the sulfolene hydrogenation reaction and improving the production efficiency.

[0039] In a specific embodiment, the main reactor 3 is a Venturi vacuum generator. As Figure 2 shown, the main reactor 3 includes a feed inlet 31, an adsorption port 32, a nozzle 33 and a discharge port 34. The feed inlet 31 is connected to the outlet end of the external circulation cooler 2 for receiving the second mixture and unreacted hydrogen. The nozzle 33 is connected to the circulation pump 5 for injecting the second mixture input by the circulation pump 5 to generate negative pressure at the adsorption port 32. The adsorption port 32 is connected to the reaction circulation tank 4 for sucking hydrogen from the reaction circulation tank 4. The discharge port 34 is connected to the reaction circulation tank 4 for transporting the liquid-phase product obtained from the second hydrogenation reaction to the reaction circulation tank 4. Specifically, as Figure 2 shown, the working principle of the Venturi vacuum generator is as follows: Hydrogen is sent into the feed inlet 31. Since the cross-section of the nozzle 33 decreases, the flow rate of hydrogen increases, the dynamic pressure increases, and the static pressure of hydrogen decreases simultaneously. Once the hydrogen passes through the nozzle 33, the accelerated air will expand and generate a vacuum. Hydrogen is sucked into the main reactor 3 through the adsorption port 32, and the hydrogen passes through the discharge port 34 and is discharged from the vacuum generator into the circulation tank together with the sucked hydrogen.

[0040] In this embodiment, the second mixture input by the circulation pump 5 is injected through the nozzle 33 to accelerate the gas flow rate, so that negative pressure is generated at the adsorption port 32, so that a large amount of hydrogen is sucked from the top of the reaction circulation tank 4 by the adsorption port 32, thereby realizing the cyclic use of hydrogen between the reaction circulation tank 4 and the main reactor 3, avoiding the loss of hydrogen, and reducing the production cost.

[0041] In a specific embodiment, the continuous hydrogenation reaction system of sulfolene further includes a hydrogen regulating valve 6 and a pressure sensor (not shown in the figure) disposed on the reaction circulation tank 4. The pressure sensor is connected to the hydrogen regulating valve 6, and the hydrogen regulating valve 6 is connected to the hydrogen inlet to adjust the valve opening degree of itself according to the pressure of the pressure sensor.

[0042] Specifically, the hydrogen regulating valve 6 includes a main valve and a pilot valve. The main valve includes a main valve disc and a piston. The pilot valve includes a valve seat, a diaphragm, and an adjusting spring. The outlet pressure is set by adjusting the pressure of the adjusting spring. The pressure change of the pressure sensor is sensed by the diaphragm. The piston is driven by the opening and closing of the pilot valve to adjust the flow area of the throttling part of the main valve, so as to achieve the function of adjusting the pressure. In the actual process of adjusting the pressure, the pressure generated by the pre-pressurization of the adjusting spring and the pressure of the gas feedback from the reaction circulation tank 4 act on the front and back sides of the internal diaphragm. The change of the pressure difference between the two will drive the opening and closing of the pilot valve. When the pressure of the adjusting spring is constant, if the gas pressure in the reaction circulation tank 4 is higher than the pressure set by the adjusting spring, the valve will close; if the gas pressure in the reaction circulation tank 4 is lower than the pressure set by the adjusting spring, the valve will open; if the gas in the reaction circulation tank 4 is equal to the pressure set by the adjusting spring, the valve will remain stationary, playing a constant pressure role; when the main reactor 3 stops using gas and there is no flow in the pipeline, the valve will automatically close.

[0043] In this embodiment, through the pressure sensor and the hydrogen regulating valve 6, the hydrogen pressure in the reaction circulation tank 4 is maintained at the optimal pressure value for the hydrogenation reaction, ensuring that the main reactor 3 can absorb hydrogen at the optimal pressure value for the second hydrogenation reaction. The second hydrogenation reaction is more complete, the hydrogen can be utilized to a greater extent, and thus the loss of hydrogen is reduced.

[0044] In a specific embodiment, the external circulation cooler 2 is provided with a first cooling medium inlet and a first cooling medium outlet. The first cooling medium passes through the external circulation cooler 2 to cool the sulfolene, hydrogen, and catalyst to reach the optimal temperature for the hydrogenation reaction, so as to better carry out the hydrogenation reaction in the main reactor 3. In this embodiment, the first cooling medium is cooling water. Of course, the first cooling medium can also be other media that can achieve the cooling effect of sulfolene, hydrogen, and catalyst.

[0045] In a specific embodiment, a cooling coil is provided inside the reaction circulation tank 4, and the inlet and outlet of the cooling coil are used to convey a second cooling medium. By the flow of the second cooling medium in the cooling coil, the reaction product is cooled, so that the reaction product is separated in the reaction circulation tank 4.

[0046] In a further embodiment, the reaction heat of the second hydrogenation reaction in the main reactor 3 is taken from the first cooling medium and the second cooling medium. Since the hydrogenation reaction is exothermic, the heat after the reaction is carried away by the first cooling medium and the second cooling medium, and then used for the reaction heat of the hydrogenation reaction in the main reactor 3, realizing the recovery and utilization of heat, saving energy, and reducing production costs; moreover, ensuring that the reaction heat of the second hydrogenation reaction is at the optimal temperature, the second hydrogenation reaction is more complete, the hydrogen can be utilized to a greater extent, and thus the loss of hydrogen is reduced.

[0047] In a specific embodiment, a liquid-phase product outlet is provided between the reaction circulation tank 4 and the circulation pump 5, and the liquid-phase product outlet is used to output the first reaction product and the second reaction product. By discharging the first reaction product and the second reaction product through the reaction product outlet, the space of the reaction circulation tank 4 can be not occupied, so that the reaction circulation tank 4 can store more hydrogen, the stable control of the hydrogen pressure can be better realized, the hydrogenation reaction is more complete, the utilization rate of hydrogen is increased, and thus the loss of hydrogen is reduced.

[0048] Embodiment 2

[0049] The embodiment of the present invention provides a continuous hydrogenation reaction method for sulfolene, including:

[0050] Step S101: A circulation pump pumps a first mixture of hydrogen, the liquid-phase product transported from the reaction circulation tank, a catalyst, and sulfolene into the auxiliary reactor.

[0051] Step S102: The auxiliary reactor conducts a first hydrogenation reaction on the first mixture and hydrogen, and transports the obtained second mixture and unreacted hydrogen to the external circulation cooler.

[0052] Step S103: The external circulation cooler cools the second mixture and unreacted hydrogen input from the auxiliary reactor and transports them to the main reactor.

[0053] Step S104: The main reactor draws hydrogen from the reaction circulation tank, and transports the input hydrogen, the second mixture, the liquid-phase product obtained by the second hydrogenation reaction of the drawn hydrogen, and unreacted hydrogen to the reaction circulation tank.

[0054] Step S105: The reaction circulation tank transports the liquid-phase product input from the main reactor to the circulation pump and / or discharges it, and supplies the unreacted hydrogen to the main reactor.

[0055] An embodiment of the present invention provides a continuous hydrogenation reaction method for sulfolene. By allowing the hydrogen remaining after the second hydrogenation reaction to enter the reaction circulation tank for storage, maintaining the hydrogen pressure in the reaction circulation tank through a hydrogen regulating valve, and sucking hydrogen from the reaction circulation tank through a main reactor, the recovery of hydrogen is achieved, the loss of hydrogen is reduced, and the production cost is lowered; sulfolene and hydrogen first undergo a first hydrogenation reaction in an auxiliary reactor under the action of a catalyst, and then continue to undergo a second hydrogenation reaction in the main reactor. The conversion rate of sulfolene can be maintained at a relatively high level, more products are obtained from the hydrogenation reaction, hydrogen can be utilized to a greater extent, and thus the loss of hydrogen is reduced; continuous production of the hydrogenation reaction of sulfolene is also realized, and the production efficiency is improved.

[0056] In some embodiments, the catalyst uses a homogeneous organonickelate catalyst. The catalyst can be one or a mixture of nickel naphthenate and nickel neodecanoate, and the diluting solvent of the catalyst is cyclopentane, cyclohexane, etc.

[0057] The above continuous hydrogenation reaction method for sulfolene has the following two sets of data:

[0058] (1) The feeding rate of sulfolene is 1000 kg / h, the feeding rate of hydrogen is 16.7 kg / h, the concentration of nickel naphthenate in the catalyst is 1000 ppm, the pressure in the main reactor is 2.7 MPa, the temperature after the external circulation cooler is 65 °C, the temperature of the medium in the reaction circulation tank is maintained at 65 °C, the conversion rate of sulfolene is 99.2%, and the conversion rate of hydrogen is close to 100%;

[0059] (2) The feeding rate of sulfolene is 1500 kg / h, the feeding rate of hydrogen is 25.02 kg / h, the concentration of nickel decanoate in the catalyst is 1500 ppm, the pressure in the main reactor is 2.7 MPa, the temperature after the external circulation cooler is 65 °C, the temperature of the medium in the reaction circulation tank is maintained at 65 °C, the conversion rate of sulfolene is 99.2%, and the conversion rate of hydrogen is close to 100%.

[0060] The above two sets of data show that the above continuous hydrogenation reaction method for sulfolene can significantly improve the conversion rate of sulfolene, more products are obtained from the hydrogenation reaction, and the production efficiency can be further improved.

[0061] Example Three

[0062] An embodiment of the present invention provides an application of the continuous hydrogenation reaction system for sulfolene described in Example 1 in the preparation of sulfolane.

[0063] The embodiment of the present invention provides an application of a continuous hydrogenation reaction system of sulfolene in the preparation of sulfolane. By storing the hydrogen remaining from the second hydrogenation reaction in the reaction recycle tank, maintaining the hydrogen pressure in the reaction recycle tank through a hydrogen regulating valve, and sucking hydrogen from the reaction recycle tank by the main reactor, the recovery of hydrogen is achieved, the loss of hydrogen is reduced, and the production cost is lowered. First, sulfolene and hydrogen react in the auxiliary reactor under the action of a catalyst to carry out the first hydrogenation reaction, and then continue to carry out the second hydrogenation reaction in the main reactor. The conversion rate of sulfolene can be maintained at a relatively high level, more products are obtained from the hydrogenation reaction, hydrogen can be utilized to a greater extent, and thus the loss of hydrogen is reduced.

[0064] Example 4

[0065] The embodiment of the present invention provides an application of the continuous hydrogenation reaction method of sulfolene described in Example 2 in the preparation of sulfolane.

[0066] In the above detailed description, various features are combined in a single embodiment to simplify the present disclosure. This method of disclosure should not be construed as reflecting an intention that the embodiments of the claimed subject matter require more features than are expressly recited in each claim. On the contrary, as reflected in the appended claims, the present invention lies in a state with fewer features than all the features of the single disclosed embodiment. Therefore, the appended claims are hereby expressly incorporated into the detailed description, where each claim stands alone as a separate preferred embodiment of the present invention.

[0067] The above description includes examples of one or more embodiments. Of course, it is impossible to describe all possible combinations of components or methods for the purpose of describing the above embodiments, but those of ordinary skill in the art should recognize that the various embodiments can be further combined and arranged. Therefore, the embodiments described herein are intended to cover all such changes, modifications, and variations that fall within the scope of the appended claims. In addition, with respect to the term "comprising" used in the specification or claims, this term is covered in a manner similar to the term "including" as interpreted when "including" is used as a transitional word in the claims. In addition, any use of the term "or" in the claims or the specification is intended to mean "non-exclusive or".

Claims

1. A continuous hydrogenation reaction system for sulfolene, characterized in that, It includes a circulation pump, an auxiliary reactor, an external circulation cooler, a main reactor and a reaction circulation tank, wherein: The circulation pump has an input end connected to the reaction circulation tank and an output end connected to the auxiliary reactor. A hydrogen inlet, a sulfolene inlet and a catalyst inlet are arranged between the circulation pump and the auxiliary reactor, and are used for pumping a first mixture obtained by mixing hydrogen, the liquid-phase product transported from the reaction circulation tank, the catalyst and sulfolene into the auxiliary reactor; The auxiliary reactor is connected to the circulation pump and the external circulation cooler at both ends respectively, and is used for carrying out a first hydrogenation reaction on the first mixture and hydrogen, and transporting the obtained second mixture and unreacted hydrogen to the external circulation cooler; The external circulation cooler has an inlet end connected to the auxiliary reactor and an outlet end connected to the main reactor, so as to cool the second mixture and unreacted hydrogen input from the auxiliary reactor and transport them to the main reactor; The main reactor is connected to the reaction circulation tank, and is used for sucking hydrogen from the reaction circulation tank, and transporting the liquid-phase product and unreacted hydrogen obtained by carrying out a second hydrogenation reaction on the input hydrogen, the second mixture and the sucked hydrogen to the reaction circulation tank; the main reactor is a Venturi vacuum generator, and the main reactor includes a feed inlet, an adsorption port, a nozzle and a discharge port. The feed inlet is connected to the outlet end of the external circulation cooler and is used for receiving the second mixture and unreacted hydrogen; the nozzle is connected to the circulation pump and is used for spraying the second mixture input by the circulation pump so as to generate negative pressure at the adsorption port; the adsorption port is connected to the reaction circulation tank and is used for sucking hydrogen from the reaction circulation tank; the discharge port is connected to the reaction circulation tank and is used for transporting the liquid-phase product obtained by the second hydrogenation reaction to the reaction circulation tank; The reaction circulation tank is connected to the main reactor and the circulation pump respectively, and is used for transporting the liquid-phase product input from the main reactor to the circulation pump and / or discharging it, and supplying unreacted hydrogen to the main reactor.

2. The continuous hydrogenation reaction system of sulfolene according to claim 1, wherein It further includes a hydrogen regulating valve and a pressure sensor arranged on the reaction circulation tank. The pressure sensor is connected to the hydrogen regulating valve, and the hydrogen regulating valve is connected to the hydrogen inlet, so as to adjust the valve opening of itself according to the pressure of the pressure sensor.

3. The continuous hydrogenation reaction system of sulfolene according to claim 2, characterized in that, The external circulation cooler is provided with a first cooling medium inlet and a first cooling medium outlet.

4. The continuous hydrogenation reaction system of sulfolene according to claim 3, wherein, A cooling coil is arranged inside the reaction circulation tank, and the inlet and outlet of the cooling coil are used for transporting a second cooling medium.

5. The continuous hydrogenation reaction system of sulfolene according to claim 4, wherein, A liquid-phase product outlet is arranged between the reaction circulation tank and the circulation pump, and the liquid-phase product outlet is used for outputting the liquid-phase product.

6. Application of the continuous hydrogenation reaction system of sulfolene according to any one of claims 1-5 in the preparation of sulfolane.

7. A continuous hydrogenation reaction method of sulfolene, using the continuous hydrogenation reaction system of sulfolene described in any one of claims 1-5, characterized in that, It includes: The circulation pump pumps a first mixture obtained by mixing hydrogen, the liquid-phase product transported from the reaction circulation tank, the catalyst and sulfolene into the auxiliary reactor; The first hydrogenation reaction is carried out on the first mixture and hydrogen by an auxiliary reactor, and the obtained second mixture and unreacted hydrogen are transported to the external circulation cooler; The second mixture and unreacted hydrogen input from the auxiliary reactor are cooled by the external circulation cooler and transported to the main reactor; The main reactor sucks hydrogen from the reaction circulation tank, and the hydrogen, the second mixture and the hydrogen sucked are subjected to a second hydrogenation reaction to obtain a liquid-phase product and unreacted hydrogen, which are transported to the reaction circulation tank; The reaction circulation tank transports the liquid-phase product input from the main reactor to the circulation pump and / or discharges it, and provides the unreacted hydrogen to the main reactor.

8. The continuous hydrogenation reaction method of sulfolene according to claim 7, characterized in that, The catalyst is a homogeneous organonickelate catalyst.

9. Use of the continuous hydrogenation reaction method of sulfolene according to claim 7 or 8 in the preparation of sulfolane.

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