Vinyl chloride gas-liquid phase production device

Abstract

The utility model provides a vinyl chloride gas-liquid phase production device. The vinyl chloride gas-liquid phase production device comprises a preheating mixer, a microreactor, a separation tower, a condenser and a crude vinyl chloride storage tank which are sequentially connected along the material flowing direction, an ionic liquid catalyst inlet is formed in the bottom of the micro-reactor, the top of the micro-reactor is communicated with the bottom of the separating tower through a connecting section, a micro-reactor material outlet is formed in the top wall of the micro-reactor, and an annular overflow baffle is arranged on the periphery of the micro-reactor material outlet; an annular cavity for containing an ionic liquid catalyst is formed between the annular overflow baffle and the inner wall of the connecting section, an ionic liquid catalyst outlet is formed in the side wall of the connecting section, and an ionic liquid catalyst outer circulation pipeline is arranged between the ionic liquid catalyst outlet and the ionic liquid catalyst inlet. The device can realize full mixing of mixed gas raw materials and timely removal of reaction heat, improves the selectivity of vinyl chloride, reduces the generation of byproducts, and improves the purity of vinyl chloride products.

Description

Technical Field

[0001] The utility model relates to a vinyl chloride production device, in particular to a gas-liquid phase production device for vinyl chloride. Background Art

[0002] Vinyl chloride is an important monomer used in polymer chemical industry and can be prepared from ethylene or acetylene. As is well known, vinyl chloride is a toxic substance. It forms an explosive mixture with air and is more likely to explode under the action of external pressure. During storage and transportation, the tightness of the container and nitrogen sealing must be noted, and a small amount of polymerization inhibitor should be added. The preparation method of vinyl chloride is also extremely special. According to the raw material route, it can be divided into calcium carbide acetylene method and ethylene ethane method. The calcium carbide method uses calcium carbide to react with water to generate acetylene. In a fixed-bed reactor, with activated carbon supported HgCl 2 as a catalyst, acetylene and hydrogen chloride undergo a hydrochlorination reaction to form vinyl chloride monomer. However, this reaction is a strongly exothermic reaction. If a traditional fixed-bed reactor is used to produce vinyl chloride, it will cause local overheating on the surface of the activated carbon supported HgCl 2 catalyst, carbon deposition will block the pores, reduce the contact area between the catalyst and the gas, cause rapid deactivation of the catalyst, and reduce the catalytic efficiency of the catalyst. In addition, it will also cause local temperature runaway of the equipment, increase side reactions, increase the types and quantities of by-products, make it difficult to refine subsequent products, and affect the product quality.

[0003] Patent CN209508087U discloses a vinyl chloride synthesis system for improving product purity. This technical solution uses a mercury catalyst as a solid catalyst and replaces the fixed-bed reactor with a microreactor. The hydraulic diameter of the reaction microchannel is only 0.1 - 5 mm, and the catalyst particles are filled into the microchannel to form a packed bed. The solid mercury catalyst is filled in the microchannel with a diameter of 0.1 - 5 mm, and the filling difficulty is high. Moreover, the subsequent mercury collection is required after using the mercury catalyst, resulting in an increase in equipment investment and the complexity of the process flow. The use of mercury catalyst will also cause environmental pollution.

[0004] Currently, the research on liquid catalysts has become a hot topic in the industry, and the research on vinyl chloride reaction devices suitable for liquid catalysts has also become an important research direction in this field. Summary of the Utility Model

[0005] The purpose of the utility model is to provide a gas-liquid phase production device for vinyl chloride to solve the problems of local temperature runaway, low catalytic efficiency, many by-products, complex process flow, high equipment investment, etc. in the existing vinyl chloride production devices.

[0006] To achieve the above object, the present utility model provides the following technical solution. A vinyl chloride gas-liquid phase production device includes a preheating mixer, a micro-reactor, a separation tower, a condenser, and a crude vinyl chloride storage tank connected in sequence along the material flow direction. An ionic liquid catalyst inlet is provided at the bottom of the micro-reactor. The top of the micro-reactor is communicated with the bottom of the separation tower through a connection section. A micro-reactor material outlet is opened on the top wall of the micro-reactor, and an annular overflow baffle is provided outside the micro-reactor material outlet. An annular cavity for accommodating the ionic liquid catalyst is formed between the annular overflow baffle and the inner wall of the connection section. An ionic liquid catalyst outlet for discharging the ionic liquid catalyst retained in the annular cavity is provided on the side wall of the connection section. An ionic liquid catalyst external circulation pipeline is provided between the ionic liquid catalyst outlet and the ionic liquid catalyst inlet.

[0007] A first mixed gas inlet is provided at the bottom of the preheating mixer. A mixed gas outlet and a temperature monitoring port inside the preheating mixer are provided at the top of the preheating mixer. A jacket is provided outside the preheating mixer, and a heat source inlet, a heat source outlet, and a temperature monitoring port of the preheating mixer jacket are provided on the jacket. A gas mixing component is provided inside the preheating mixer.

[0008] The gas mixing component is composed of multiple groups of helices with spiral bends symmetrically distributed, or multiple groups of helices intersecting each other, or multiple groups of triangular bodies with a certain angle distributed vertically and horizontally, or multiple groups of distributed bodies composed of two trapezoids with a certain angle, or multiple groups of distributed bodies composed of two triangles with a certain angle, or other structural bodies that play a role in gas mixing.

[0009] The first mixed gas inlet of the preheating mixer is connected to one end of a first mixed gas pipeline, and the other end of the first mixed gas pipeline is respectively connected to a hydrogen chloride gas pipeline and an acetylene gas pipeline. The mixed gas outlet at the top of the preheating mixer is connected to a second mixed gas inlet at the bottom of the micro-reactor through a second mixed gas pipeline.

[0010] Preferably, a regulating valve is provided on the second mixed gas pipeline. A regulating valve, a hydrogen chloride gas flow monitoring port, and a hydrogen chloride gas pressure monitoring port are installed on the hydrogen chloride gas pipeline. A regulating valve, an acetylene gas flow monitoring port, and an acetylene gas pressure monitoring port are installed on the acetylene gas pipeline. Pressure monitors are installed on all gas pressure monitoring ports, temperature monitors are installed on all temperature monitoring ports, and flow monitors are installed on all gas flow monitoring ports.

[0011] An exchanger, a catalyst storage tank, and a second delivery pump are successively arranged on the external circulation pipeline of the ionic liquid catalyst along the catalyst flow direction. The ionic liquid catalyst enters the microreactor through the ionic liquid catalyst inlet. After catalyzing the reaction of the mixed raw material gas, it flows out from the ionic liquid catalyst outlet to the external circulation pipeline of the ionic liquid catalyst, passes through the exchanger, and then returns to the catalyst storage tank. Under the action of the second delivery pump, it enters the microreactor again to continue participating in the reaction, realizing circulation.

[0012] A catalyst addition port is arranged at the top of the catalyst storage tank, and the catalyst addition port is connected to the catalyst feeding pipeline. The catalyst feeding pipeline is used to add the ionic liquid catalyst before starting up and supplement the ionic liquid catalyst during the start-up process; the catalyst storage tank is used to maintain the balance of the ionic liquid catalyst in the microreactor to ensure the smooth progress of the acetylene hydrochlorination reaction.

[0013] There is at least one microreaction channel in the microreactor. The diameter of the microreaction channel is 10∽300 μm. The feed ports of each microreaction channel converge together to form the microreactor material inlet, and the outlets of each microreaction channel converge together to form the microreactor material outlet; a second mixed gas inlet is arranged at the bottom of the microreactor, and both the second mixed gas inlet and the ionic liquid catalyst inlet are communicated with the microreactor material inlet. A cold source inlet, a microreactor temperature monitoring port, and a microreactor pressure monitoring port are arranged on the upper side of the microreactor, and a cold source outlet is arranged on the lower side of the microreactor.

[0014] The exchanger on the external circulation pipeline of the ionic liquid catalyst and the cold source inlet and cold source outlet arranged on the microreactor are used together to quickly remove the reaction heat released by the acetylene hydrochlorination reaction in a timely manner, so that the reaction temperature meets the process requirements and is easy to control, making the equipment operation safe and stable, reducing side reactions, and improving the selectivity of vinyl chloride.

[0015] Preferably, an ionic liquid catalyst external circulation pipeline temperature monitoring port, an ionic liquid catalyst flow monitoring port, and a regulating valve are also arranged on the external circulation pipeline of the ionic liquid catalyst.

[0016] A vinyl chloride gas outlet is arranged at the top of the separation tower, and a separation tower top temperature monitoring port and a separation tower top pressure monitoring port are arranged on the upper side.

[0017] The separation tower can be a plate tower, a packed tower, or other separation towers that can play a separation role, preferably a packed tower; trays or packing are arranged inside the separation tower.

[0018] The feed inlet of the condenser is connected to the vinyl chloride gas outlet of the separation column, and the discharge outlet of the condenser is connected to the crude vinyl chloride storage tank through a pipeline. At least one condenser is provided. The cold source outlet of the first condenser is connected to the heat source inlet of the preheating mixer, and the cold source inlet of the first condenser is connected to the heat source outlet of the preheating mixer.

[0019] The working principle of the present utility model: The preheating mixer can fully mix and preheat the raw material mixed gas; the microreactor is provided with micron-scale microreaction channels, which can fully mix a small amount of hydrogen chloride gas, acetylene gas and ionic liquid catalyst, reduce the occurrence of side reactions and reduce by-products; the separation column is internally provided with trays or packings, which can separate the vinyl chloride gas and ionic liquid catalyst in the reaction liquid; the condenser can condense the vinyl chloride gas and can also provide heat source for the preheating mixer, reducing energy consumption; the ionic liquid catalyst can be recycled in the external circulation pipeline, reducing the catalyst dosage and cost.

[0020] The beneficial effects of the present utility model:

[0021] The annular overflow baffle arranged outside the material outlet of the microreactor is used to overflow the ionic liquid catalyst in the reaction liquid out of the microreactor through the ionic liquid catalyst outlet, and is recycled back into the microreactor through the ionic liquid catalyst external circulation pipeline arranged outside the microreactor and the ionic liquid catalyst inlet at the bottom of the microreactor, realizing the continuous circulation of the ionic liquid catalyst, timely removing the reaction heat released by the reaction, and enabling the continuous progress of the acetylene hydrochlorination reaction.

[0022] The microreactor can accurately mix hydrogen chloride and acetylene in proportion, and can make the molar ratio of hydrogen chloride gas and acetylene gas reach 1:1, avoiding the need to set up subsequent water washing towers and alkali washing towers due to excessive hydrogen chloride gas, simplifying the process flow, reducing equipment investment, and at the same time reducing side reactions. Compared with the prior art, it avoids problems such as an increase in by-product dichloroethane and a decrease in vinyl chloride selectivity caused by excessive hydrogen chloride, thereby improving the purity of vinyl chloride products. Moreover, the dosage of the ionic liquid catalyst is also relatively reduced, reducing the catalyst dosage and application cost.

[0023] The cold source inlets and cold source outlets arranged on the ionic liquid catalyst external circulation pipeline and the microreactor can work together to quickly remove the reaction heat in a timely manner, make the reaction temperature meet the process requirements, be easy to control, realize the safe and stable operation of the equipment, and reduce the effect of side reactions. Description of the Drawings

[0024] Figure 1 It is a schematic structural diagram of the present utility model.

[0025] Figure 2 It is a schematic structural diagram of the present utility model when two condensers are provided.

[0026] Figure 3 This is a schematic structural view of the preheating mixer of the present utility model.

[0027] Figure 4 This is a schematic structural view of the gas mixing component in the preheating mixer of the present utility model, where a, b, c, d, and e are respectively five schematic structural views of the gas mixing component.

[0028] Figure 5 This is a schematic structural view of the microreactor and the separation tower of the present utility model.

[0029] Figure 6 This is a schematic top view of the material outlet, overflow baffle, and ionic liquid catalyst outlet of the microreactor of the present utility model.

[0030] Figure 7 This is a schematic structural view of the catalyst storage tank of the present utility model.

[0031] In the figure: 1. Preheating mixer; 101. First mixed gas inlet; 102. Heat source inlet; 103. Mixed gas outlet; 104. Jacket; 105. Gas mixing component; 106. Heat source outlet;

[0032] 2. Microreactor; 21. Second mixed gas inlet; 22. Ionic liquid catalyst inlet; 23. Cold source inlet; 24. Ionic liquid catalyst outlet; 25. Vinyl chloride gas outlet; 26. Tray or packing; 27. Microreactor material outlet; 28. Overflow baffle; 29. Cold source outlet;

[0033] 3. Separation tower; 4. Condenser; 5. Crude vinyl chloride storage tank; 6. First transfer pump; 7. Heat exchanger;

[0034] 8. Catalyst storage tank; 801. Catalyst addition port; 802. Return catalyst inlet; 803. Catalyst outlet; L2. Catalyst storage tank liquid level monitoring port;

[0035] 9. Second transfer pump; 11. Hydrogen chloride gas pipeline; 12. Acetylene gas pipeline; 13. First mixed gas pipeline; 14. Second mixed gas pipeline; 15. Catalyst feeding pipeline; 16. Ionic liquid catalyst external circulation pipeline; 17. Connection section; 18. Crude vinyl chloride pipeline;

[0036] P1, hydrogen chloride gas pressure monitoring port; P2, acetylene gas pressure monitoring port; P3, micro-reactor pressure monitoring port; P4, top pressure monitoring port of the separation column; T1, micro-reactor temperature monitoring port; T2, top temperature monitoring port of the separation column; T3, jacket temperature monitoring port of the preheating mixer; T4, internal temperature monitoring port of the preheating mixer; T5, temperature monitoring port of the external circulation pipeline of the ionic liquid catalyst; T6, outlet temperature monitoring port of the condenser; T7, temperature monitoring port of the catalyst storage tank; F1, hydrogen chloride gas flow monitoring port; F2, acetylene gas flow monitoring port; F3, ionic liquid catalyst flow monitoring port; L1, liquid level monitoring port of the crude vinyl chloride storage tank; L2, liquid level monitoring port of the catalyst storage tank. Detailed implementation manners

[0037] The technical solutions in the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings.

[0038] As Figure 1 shown, a vinyl chloride gas-liquid phase production device of the present utility model includes a preheating mixer 1, a micro-reactor 2, a separation column 3, a condenser 4, a crude vinyl chloride storage tank 5, and an external circulation pipeline 16 of an ionic liquid catalyst.

[0039] The preheating mixer 1 is used to fully mix hydrogen chloride gas and acetylene gas and preheat the mixed gas to the process required temperature. As Figure 1 and 3 shown, a first mixed gas inlet 101 is provided at the bottom of the preheating mixer 1, and a mixed gas outlet 103 and an internal temperature monitoring port T4 of the preheating mixer are provided at the top. The first mixed gas inlet 101 is connected to one end of a first mixed gas pipeline 13, and the other end of the first mixed gas pipeline 13 is connected to a hydrogen chloride gas pipeline 11 and an acetylene gas pipeline 12. The two gases of hydrogen chloride and acetylene are mixed and pass through the first mixed gas pipeline 13, enter the preheating mixer 1 from the first mixed gas inlet 101, and flow out from the mixed gas outlet 103 after preheating and full mixing. A regulating valve, a hydrogen chloride gas flow monitoring port F1, and a hydrogen chloride gas pressure monitoring port P1 are installed on the hydrogen chloride gas pipeline 11, and a regulating valve, an acetylene gas flow monitoring port F2, and an acetylene gas pressure monitoring port P2 are installed on the acetylene gas pipeline 12.

[0040] A jacket 104 is sleeved outside the preheating mixer 1, and a heat source inlet 102, a heat source outlet 106, and a jacket temperature monitoring port T3 of the preheating mixer are provided on the jacket 104. A gas mixing component 105 is provided inside the preheating mixer 1.

[0041] As Figure 4 shown, the gas mixing component 105 is composed of multiple groups of helices with a spiral bent shape symmetrically distributed (as Figure 4 a), or composed of multiple groups of helices that cross each other (asFigure 4 b), or composed of triangular bodies with a certain angle distributed crosswise up and down (such as Figure 4 c), or composed of multiple sets of distributed bodies of two trapezoids formed by a certain angle (such as Figure 4 d), or composed of multiple sets of distributed bodies of two triangles formed by a certain angle (such as Figure 4 e), and can also be composed of other structural bodies that can play a role in gas mixing. The specific structure is not limited in this utility model.

[0042] The microreactor 2 is used to provide a reaction site. Inside the microreactor 2, the mixed gas of hydrogen chloride and acetylene reacts under the action of an ionic liquid catalyst to produce vinyl chloride. Such as Figure 1 、 5 and shown in 6, the bottom of the microreactor 2 is provided with a second mixed gas inlet 21 and an ionic liquid catalyst inlet 22, the top is provided with a microreactor material outlet 27, the upper side is provided with a cold source inlet 23, a microreactor temperature monitoring port T1, and a microreactor pressure monitoring port P3, the lower side is provided with a cold source outlet 29. The second mixed gas inlet 21 is connected to the mixed gas outlet 103 of the preheating mixer 1 through the second mixed gas pipeline 14, and a regulating valve is provided on the second mixed gas pipeline 14. The microreactor material outlet 27 communicates with the bottom inlet of the separation tower 3, and an annular overflow baffle 28 is provided outside the microreactor material outlet 27. An ionic liquid catalyst outlet 24 is provided on the outer wall of the connection section 17 between the microreactor 2 and the separation tower 3, and the setting position of the ionic liquid catalyst outlet 24 is lower than the top edge of the annular overflow baffle 28.

[0043] Such as Figure 1 and 6 shown, the annular overflow baffle 28 is used to overflow the ionic liquid catalyst in the reaction liquid generated by the acetylene hydrochlorination reaction to the outside of the microreactor 2, and return it to the microreactor 2 through the ionic liquid catalyst outlet 24, the ionic liquid catalyst external circulation pipeline 16, and the ionic liquid catalyst inlet 22 at the bottom of the microreactor 2, realizing the continuous circulation of the ionic liquid catalyst, removing the reaction heat released by the reaction in time, and enabling the continuous progress of the acetylene hydrochlorination reaction.

[0044] One set or multiple sets in parallel of the microreactor 2 are provided. At least one microreaction channel is provided in each microreactor 2. The diameter of the microreaction channel is 10∽300μm. The number of channels in the microreactor 2 and the number of microreactors 2 are calculated based on the volume of hydrogen chloride gas and acetylene gas. The inlets of all microreaction channels converge together to form a microreactor material inlet, and the microreactor material inlet is respectively connected to the second mixed gas inlet 21 and the ionic liquid catalyst inlet 22; the outlets of all microreaction channels converge together to form a microreactor material outlet 27.

[0045] Such asFigure 1 and 5 As shown in 5 , the separation tower 3 is located above the micro-reactor 2 and is connected to the micro-reactor 2 through the connection section 17. At the top of the separation tower 3, there is a vinyl chloride gas outlet 25, and on the upper side, there are a separation tower top temperature monitoring port T2 and a separation tower top pressure monitoring port P4. Inside the separation tower 3, there are trays or packings 26. The separation tower 3 can be a plate tower, a packed tower, or other types of separation towers that can play a separation role, preferably a packed tower.

[0046] The separation tower 3 is used to separate the vinyl chloride gas and the entrained ionic liquid catalyst in the reaction liquid discharged from the micro-reactor material outlet 27. The vinyl chloride gas is discharged from the vinyl chloride gas outlet 25, and the ionic liquid catalyst falls back and enters the ionic liquid catalyst outer circulation pipeline 16 through the ionic liquid catalyst outlet 24.

[0047] As Figure 1 shown, on the ionic liquid catalyst outer circulation pipeline 16, there are a heat exchanger 7, a catalyst storage tank 8, a second delivery pump 9, an ionic liquid outer circulation pipeline temperature monitoring port T5, an ionic liquid catalyst flow monitoring port F3, and a regulating valve. In the separation tower 3, the ionic liquid catalyst is separated from the vinyl chloride gas and falls back, flowing out from the ionic liquid catalyst outlet 24 and entering the heat exchanger 7 for heat exchange. The heat exchanger 7 quickly removes the reaction heat released by the acetylene hydrochlorination reaction, making the reaction temperature meet the process requirements and easy to control, ensuring the safe and stable operation of the equipment, reducing side reactions, and improving the selectivity of vinyl chloride. Under the action of the second delivery pump 9, the ionic liquid catalyst can enter the micro-reactor 2 again to participate in the reaction.

[0048] The catalyst storage tank 8 is used to maintain the balance of the ionic liquid catalyst in the micro-reactor 2 and ensure the smooth progress of the acetylene hydrochlorination reaction. As Figure 1 、 7 shown, on the upper part of the catalyst storage tank 8, there are a catalyst addition port 801 and a reflux catalyst inlet 802, and on the lower part, there is a catalyst outlet 803. Among them, the catalyst addition port 801 is connected to the catalyst feeding pipeline 15, and the catalyst feeding pipeline 15 is used to add ionic liquid catalyst before starting up and to supplement ionic liquid catalyst during the start-up process. In addition, the catalyst storage tank 8 is also equipped with a catalyst storage tank liquid level monitoring port L2 and a catalyst storage tank temperature monitoring port T7.

[0049] The condenser 4 is used to condense the vinyl chloride gas discharged from the vinyl chloride gas outlet 25 to obtain crude vinyl chloride. The feed inlet of the condenser 4 is connected to the vinyl chloride gas outlet 25 of the separation tower 3 through a pipeline, and the discharge outlet is connected to the crude vinyl chloride storage tank 5 through a pipeline. On the pipeline connected to the discharge outlet of the condenser 4, there is also a condenser outlet temperature monitoring port T6. At least one condenser 4 is provided, preferably two. As Figure 2As shown, when two condensers are provided, the cold source outlet of the first condenser is connected to the heat source inlet of the preheating mixer 1, and the cold source inlet of the first condenser is connected to the heat source outlet of the preheating mixer 1. The heat of the condenser can be used as the heat source of the preheating mixer 1.

[0050] The crude vinyl chloride storage tank 5 is connected to the discharge port of the condenser 4 through a pipeline. The lower part of the crude vinyl chloride storage tank 5 is connected to the crude vinyl chloride pipeline 18, and a first transfer pump 6 is provided on the crude vinyl chloride pipeline 18. The condenser 4 condenses the vinyl chloride gas discharged from the vinyl chloride gas outlet 25, and the obtained crude vinyl chloride is sent to the crude vinyl chloride storage tank 5, and then sent to the subsequent process for further refining by the first transfer pump 6 through the crude vinyl chloride pipeline 18.

[0051] Pressure monitors are installed on all pressure monitoring ports of the present utility model, temperature monitors are installed on all temperature monitoring ports, and flow monitors are installed on all flow monitoring ports.

[0052] The catalyst used in the present utility model is a mercury-free ionic liquid catalyst.

[0053] The materials used in the present utility model are common materials that do not react with raw materials or products, that is, the materials used are not limited.

[0054] When the embodiment of the present application is in use: The staff installs the equipment according to Figures 1 - 7 the structural form to form Figure 1 、 2 the vinyl chloride gas-liquid microreaction device shown in

[0055] After that, open the regulating valves on the hydrogen chloride gas pipeline 11 and the acetylene gas pipeline 12 to the same opening degree simultaneously, so that the hydrogen chloride gas and the acetylene gas form a mixed gas with a molar ratio of 1:1. The mixed gas is fed into the preheating mixer 1 through the first mixed gas inlet 101. In the preheating mixer 1, after the hydrogen chloride gas and the acetylene gas are fully mixed and preheated to the process requirement temperature, they are fed into the micro-reactor 2 through the second mixed gas pipeline 14, the second mixed gas inlet 21 and the micro-reactor material inlet. In the micro-reaction channels in the micro-reactor 2, the hydrogen chloride gas and the acetylene gas react under the action of an ionic liquid catalyst to generate vinyl chloride gas, and at the same time, a reaction solution is obtained. The reaction solution mainly contains vinyl chloride gas, ionic liquid catalyst, etc. Under the action of power, the reaction solution moves upward along the micro-reaction channels to the micro-reactor material outlet 27. The ionic liquid catalyst in the reaction solution overflows through the micro-reactor material outlet 27 and the annular overflow baffle 28 into the annular cavity between the annular overflow baffle 28 and the connection section 17, and is discharged through the ionic liquid catalyst outlet 24 into the ionic liquid catalyst external circulation pipeline 16. The reaction heat is quickly removed in time through the heat exchanger 7 on the ionic liquid catalyst external circulation pipeline 16 and the cold source of the micro-reactor 2 itself. The acetylene hydrochlorination reaction temperature is controllable and easy to control, and the reaction is safe and stable. At the same time, the vinyl chloride gas in the reaction solution enters the separation tower 3 upward through the connection section 17. In the separation tower 3, the vinyl chloride gas and the ionic liquid catalyst it entrains are separated. The ionic liquid catalyst falls downward, and the vinyl chloride gas is discharged through the vinyl chloride gas outlet 25 into the condenser 4 for condensation. The crude vinyl chloride obtained after condensation is fed into the crude vinyl chloride storage tank 5, and then discharged through the crude vinyl chloride pipeline 18 and sent to the subsequent process for further refining to obtain vinyl chloride products.

[0056] With the continuous addition of hydrogen chloride gas and acetylene gas, the continuous circulation of the ionic liquid catalyst, and the continuous discharge of crude vinyl chloride, the continuous, stable and safe production of vinyl chloride can be realized.

[0057] Although the present invention has been described in detail with reference to the foregoing embodiments, for those skilled in the art, they can still modify the technical solutions described in the foregoing embodiments, or perform equivalent replacements for some of the technical features. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.

Claims

1. A vinyl chloride gas-liquid phase production device, characterized in that: The invention comprises a preheating mixer, a microreactor, a separation tower, a condenser and a crude vinyl chloride storage tank which are connected in sequence along the material flow direction; an ionic liquid catalyst inlet is arranged at the bottom of the microreactor, the top of the microreactor is connected with the bottom of the separation tower through a connecting section, a microreactor material outlet is arranged on the top wall of the microreactor, and an annular overflow baffle is arranged at the periphery of the microreactor material outlet; an annular cavity for retaining the ionic liquid catalyst is formed between the annular overflow baffle and the inner wall of the connecting section, an ionic liquid catalyst outlet for discharging the ionic liquid catalyst retained in the annular cavity is arranged on the side wall of the connecting section, and an ionic liquid catalyst external circulation pipeline is arranged between the ionic liquid catalyst outlet and the ionic liquid catalyst inlet.

2. The gas-liquid phase production device of vinyl chloride according to claim 1, characterized in that: A first mixed gas inlet is provided at the bottom of the preheating mixer, and a mixed gas outlet and a temperature monitoring port inside the preheating mixer are provided at the top of the preheating mixer; a jacket is provided on the outside of the preheating mixer, and a heat source inlet, a heat source outlet and a temperature monitoring port of the preheating mixer jacket are provided on the jacket; a gas mixing component is provided inside the preheating mixer.

3. The gas-liquid phase production device of vinyl chloride according to claim 1 or 2, characterized in that: The first mixed gas inlet of the preheating mixer is connected to one end of a first mixed gas pipeline, and the other end of the first mixed gas pipeline is connected to a hydrogen chloride gas pipeline and an acetylene gas pipeline respectively; the mixed gas outlet at the top of the preheating mixer is connected to the second mixed gas inlet at the bottom of the microreactor through the second mixed gas pipeline.

4. The gas-liquid phase production device of vinyl chloride according to claim 1, characterized in that: A heat exchanger, a catalyst storage tank and a second delivery pump are arranged in sequence on the ionic liquid catalyst external circulation pipeline along the catalyst flow direction.

5. The vinyl chloride gas-liquid phase production device according to claim 1, characterized in that: The microreactor has at least one microreaction channel with a diameter of 10-300 μm. The feed ports of the microreaction channels converge to form a microreactor material inlet, and the outlets of the microreaction channels converge to form the microreactor material outlet. A second mixed gas inlet is provided at the bottom of the microreactor, and the second mixed gas inlet and the ionic liquid catalyst inlet are both connected to the microreactor material inlet.

6. The gas-liquid phase production device of vinyl chloride according to claim 1 or 5, characterized in that: A cold source inlet, a microreactor temperature monitoring port, and a microreactor pressure monitoring port are arranged on the upper side of the microreactor, and a cold source outlet is arranged on the lower side of the microreactor.

7. The gas-liquid phase production device of vinyl chloride according to claim 1, characterized in that: A vinyl chloride gas outlet is provided at the top of the separation tower, and the separation tower is a plate tower or a packed tower.

8. The gas-liquid phase production device of vinyl chloride according to claim 1 or 7, characterized in that: The feed inlet of the condenser is connected to the vinyl chloride gas outlet of the separation tower, and the discharge port of the condenser is connected to the crude vinyl chloride storage tank through a pipeline.

9. The gas-liquid phase production device of vinyl chloride according to claim 1, characterized in that: At least one condenser is provided, the cold source outlet of the first condenser is connected to the heat source inlet of the preheating mixer, and the cold source inlet of the first condenser is connected to the heat source outlet of the preheating mixer.

10. The gas-liquid phase production device of vinyl chloride according to claim 4, characterized in that: A catalyst adding port is arranged on the top of the catalyst storage tank.

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