A mixing ejector and reaction kettle for removing hydrogen chloride phase and a removal method

Abstract

The invention discloses a mixing ejector and a reactor for removing hydrogen chloride phase and a removal method, comprising a feed nozzle, a suction sleeve and a discharge nozzle, which are all installed in the reactor and arranged in sequence along the material flow direction. The flow cross section of the feed nozzle gradually decreases along the material flow direction, and the inlet of the feed nozzle is connected with a feed pipe outside the reactor. The suction sleeve is divided into a connecting section, a negative pressure section and a diffusion section in sequence along the material flow direction. The connecting section is coaxially sleeved at the outlet of the feed nozzle. A plurality of through holes connected with the inside of the reactor are provided on the connecting section. The through holes are circumferentially and evenly spaced around the outer peripheral side of the outlet of the feed nozzle. The flow cross section of the negative pressure section gradually decreases along the material flow direction, and the flow cross section of the diffusion section gradually increases in the opposite direction of the material flow. The discharge nozzle is connected at the outlet of the diffusion section, so as to overcome the defect of high energy consumption in the existing production process of removing hydrogen chloride from chloride intermediates.

Description

Technical Field

[0001] The invention relates to the technical field of hydrogen chloride removal, in particular to a mixing ejector and a reaction kettle for removing hydrogen chloride phase and a removal method. Background Art

[0002] Chloride intermediates refer to fatty acid methyl esters, straight-chain hydrocarbons, and aromatic hydrocarbons that contain about 1% hydrogen chloride gas after the chlorination reaction is completed. Before the hydrogen chloride is blown off, they are called chloride intermediates. After the hydrogen chloride is blown off with compressed gas, they are important industrial raw materials and are widely used in industries such as polyvinyl chloride, polyurethane, rubber and plastics, oil products, and pharmaceutical intermediates.

[0003] After chlorination, fatty acid methyl esters, straight-chain hydrocarbons, and aromatic hydrocarbons all need to be blown off with compressed air or nitrogen to remove the hydrogen chloride in the chloride. The current process uses a bubbling process that inserts a pipe from the center of the upper part of the chloride intermediate refining kettle. The bubbling process uses a 10m 3 / h gas compressor gas source, energy consumption 55kw / h. Although in principle, no matter how much energy is consumed and how long it takes to remove hydrogen chloride, the hydrogen chloride content in the chloride intermediate can always meet the standard, but the overall energy consumption is too high, which increases the cost of removing hydrogen chloride. Summary of the invention

[0004] The purpose of the present invention is to provide a mixing ejector and a reaction kettle for removing hydrogen chloride phase and a removal method to solve the problems existing in the above-mentioned prior art and overcome the defect of high energy consumption in the existing production process of removing hydrogen chloride from chloride intermediates.

[0005] To achieve the above-mentioned purpose, the present invention provides the following scheme: The present invention provides a mixing ejector for removing the hydrogen chloride phase, comprising a feed nozzle, a suction sleeve and a discharge nozzle, which are all installed in a reactor and arranged in sequence along the material flow direction. The flow cross-section of the feed nozzle gradually decreases along the material flow direction, and its inlet is connected to a feed pipe located outside the reactor. The suction sleeve is divided into a connecting section, a negative pressure section and a diffusion section in sequence along the material flow direction. The connecting section is coaxially sleeved at the outlet of the feed nozzle. A plurality of through holes connected to the inside of the reactor are provided on the connecting section. Each of the through holes is circumferentially and evenly spaced around the outer peripheral side of the feed nozzle outlet. The flow cross-section of the negative pressure section gradually decreases along the material flow direction, and the flow cross-section of the diffusion section gradually increases in the opposite direction of the material flow. The discharge nozzle is connected at the outlet of the diffusion section.

[0006] Preferably, the discharge nozzle is a fixed-angle spiral nozzle.

[0007] Preferably, a mixing section for mixing materials is connected between the negative pressure section and the diffusion section, and the mixing section extends along the direction of material flow.

[0008] A reactor is also provided, comprising a reactor body, a mounting hole being provided at the bottom of the reactor body, an inlet portion of the feed nozzle being sealingly mounted at the mounting hole, a chlorinated intermediate supply pipeline, a refined gas supply pipeline and a chloride product discharge pipeline being connected in parallel to the inlet of the feed nozzle, and a hydrogen chloride discharge pipeline being connected to the top of the reactor body.

[0009] Preferably, a vertically extending liquid level pipe is provided on one side of the reactor body, and both ends of the liquid level pipe are opened. The bottom opening is connected in parallel with the chloride product discharge pipeline to the inlet of the feed nozzle, and the top opening is connected in parallel with the chlorinated intermediate supply pipeline and the refined gas supply pipeline.

[0010] Preferably, a mass calibrator is connected in series on the chlorinated intermediate supply pipeline.

[0011] Preferably, the top structure of the reactor body is conical, and its radial cross section gradually decreases from bottom to top, and the hydrogen chloride discharge pipeline is connected to the top position of the reactor body.

[0012] Preferably, the hydrogen chloride discharge pipeline is connected to a gas-liquid separator, the liquid discharge port of the gas-liquid separator is connected to the reactor body, and the gas discharge port of the gas-liquid separator is connected to a hydrogen chloride gas collecting mechanism.

[0013] Preferably, the top of the reactor body is connected to a pressure balance pipeline which is distributed in parallel with the hydrogen chloride discharge pipeline, and the gas outlet of the pressure balance pipeline is connected to a chlorination reactor.

[0014] A removal method is also provided, comprising the following steps:

[0015] Online mass calibration: The chloride intermediate continuously enters the mass calibrator through the inlet of the chlorinated intermediate supply pipeline to complete the online mass calibration;

[0016] Passing in the chloride intermediate: after completing the online mass calibration, the chloride intermediate continuously enters the feed nozzle connected to the reactor body through the liquid level pipeline, and enters the reactor body through the discharge nozzle and the through hole on the connecting section, and the gas precipitated from the chloride intermediate is returned to the chlorination reactor from the air pressure balance pipeline, forming an air pressure balance in a connected state with the chlorination reactor;

[0017] Preparation before introducing refined gas: after the material in the reactor body reaches 80% of the reactor volume, close the chlorinated intermediate supply pipeline, close the gas pressure balance pipeline, and close the liquid outlet of the gas-liquid separator;

[0018] Introducing refined gas: opening the refined gas supply pipeline, guiding the refined gas from the feed nozzle into the reactor body, the refined gas flows through the negative pressure section, and generates negative pressure at the negative pressure section, and the chlorinated intermediate in the reactor body is reversely sucked into the negative pressure section from the through hole of the connecting section, and the chlorinated intermediate is mixed with the refined gas in the negative pressure section and the mixing section. During the mixing process, the saturated hydrogen chloride gas in the chlorinated intermediate is precipitated and ejected from the discharge nozzle together with the chlorinated intermediate and the refined gas, the saturated hydrogen chloride gas and the refined gas float up and flow into the hydrogen chloride discharge pipeline, and are discharged into the hydrogen chloride gas collection mechanism after being purified by the gas-liquid separator.

[0019] Compared with the prior art, the present invention has achieved the following technical effects:

[0020] When the refined gas enters the negative pressure section, a Venturi effect is generated, and a negative pressure zone is formed in the negative pressure section. After the chloride intermediate is poured into the reactor, the refined gas is introduced into the reactor through the feed nozzle. The refined gas generates negative pressure in the negative pressure section, and the chloride intermediate in the reactor is reversely sucked into the negative pressure section through the through hole of the connecting section, so that the refined gas and the chloride intermediate are mixed in the negative pressure section and the diffusion section. During the mixing process, the saturated hydrogen chloride gas in the chloride intermediate is precipitated and mixed with the refined gas, and at the same time, it is strongly ejected from the diffusion section and the discharge nozzle together with the chloride intermediate. The ejected liquid and gas mixture presents a film state, and the mixed hydrogen chloride gas floats from the liquid to achieve the work of precipitating hydrogen chloride. The chloride intermediate is internally circulated in the reactor body through the discharge nozzle and the through hole of the connecting section, which plays a role of full stirring, accelerates the removal speed of hydrogen chloride in the chloride intermediate, creates conditions for continuous chlorination production, and omits the feeding pump of the chloride intermediate, thereby overcoming the defect of high energy consumption in the existing chloride intermediate removal hydrogen chloride production process. In the chloride intermediate removal hydrogen chloride production process, the energy consumption is greatly reduced by 80%, which is of great significance to energy conservation and emission reduction in this field. BRIEF DESCRIPTION OF THE DRAWINGS

[0021] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative labor.

[0022] Figure 1 It is a schematic diagram of the overall structure of the reactor of the present invention;

[0023] Figure 2It is a schematic diagram of the structure of the mixing ejector of the present invention;

[0024] Among them, 1-refined gas supply pipeline, 2-chlorinated intermediate supply pipeline, 3-mass calibrator, 4-air pressure balance pipeline, 5-hydrogen chloride discharge pipeline, 6-gas-liquid separator, 7-stabilizer inlet, 8-chloride finished product collection mechanism, 9-material pump, 10-chloride finished product discharge pipeline, 11-mixing injector, 12-reactor body, 13-liquid level pipeline, 14-sampling point, 15-discharge nozzle, 16-diffusion section, 17-mixing section, 18-negative pressure section, 19-through hole, 20-connecting section, 21-feed nozzle. DETAILED DESCRIPTION

[0025] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0026] The purpose of the present invention is to provide a mixing ejector and a reaction kettle for removing hydrogen chloride phase and a removal method to solve the problems existing in the above-mentioned prior art and overcome the defect of high energy consumption in the existing production process of removing hydrogen chloride from chloride intermediates.

[0027] In order to make the above-mentioned objects, features and advantages of the present invention more obvious and easy to understand, the present invention is further described in detail below with reference to the accompanying drawings and specific embodiments.

[0028] like Figure 1 to Figure 2As shown, this embodiment provides a mixing ejector for removing the hydrogen chloride phase, including a feed nozzle 21, a suction sleeve and a discharge nozzle 15, which are all installed in the reactor and arranged in sequence along the material flow direction. The flow cross-section of the feed nozzle 21 gradually decreases along the material flow direction, and its inlet is connected to a feed pipe located outside the reactor. The suction sleeve is divided into a connecting section 20, a negative pressure section 18 and a diffusion section 16 in sequence along the material flow direction. The connecting section 20 is coaxially sleeved at the outlet of the feed nozzle 21. A plurality of through holes 19 connected to the inside of the reactor are opened on the connecting section 20, and each through hole 19 surrounds the feed nozzle 21 at equal intervals along the circumferential direction. 1, as a preferred embodiment, the number of through holes 19 is not less than four, and the discharge nozzle 15 is combined to discharge the material, so that the chloride intermediate passing through the feed nozzle 21 is divided into at least five paths to form a multi-channel spring state, and enters the reactor, so that the chloride intermediate can be fully surged to precipitate the gas inside it, and the surging chloride intermediate generates temperature difference convection, which fully stirs the chloride intermediate in the reactor to make its temperature uniform. When the chloride intermediate convects, hydrogen chloride in the chloride intermediate is precipitated to form hydrogen chloride bubbles, and preferably the chloride intermediate liquid phase is discharged in time to accelerate the process of removing hydrogen chloride from the chloride intermediate.

[0029] Moreover, the flow cross section of the negative pressure section 18 gradually decreases along the direction of material flow, and the flow cross section of the diffusion section 16 gradually increases in the opposite direction of material flow, and the discharge nozzle 15 is connected to the outlet of the diffusion section 16. When the refined gas enters the negative pressure section 18, a Venturi effect is generated, and a negative pressure zone is formed in the negative pressure section 18. After the chloride intermediate is poured into the reactor, the refined gas is introduced into the reactor through the feed nozzle 21, and the refined gas generates a negative pressure in the negative pressure section 18, and the chloride intermediate in the reactor is reversely sucked into the negative pressure section 18 through the through hole 19 of the connecting section 20, so that the refined gas and the chloride intermediate are mixed in the negative pressure section 18 and the diffusion section 16. During the mixing process, the saturated hydrogen chloride gas in the chloride intermediate is precipitated and mixed with the refined gas, and at the same time, it is strongly ejected from the diffusion section 16 and the discharge nozzle 15 together with the chloride intermediate, and the ejected liquid and gas mixture presents a film state, and the mixed hydrogen chloride gas floats from the liquid to achieve the work of precipitating hydrogen chloride. Furthermore, the chloride intermediate generates internal circulation in the reactor body 12 through the discharge nozzle 15 and the through hole 19 of the connecting section 20, which plays a role of full stirring, accelerates the removal speed of hydrogen chloride in the chloride intermediate, creates conditions for continuous chlorination production, and omits the feeding pump of the chloride intermediate, thereby overcoming the defect of high energy consumption in the existing chloride intermediate removal hydrogen chloride production process. In addition, in the chloride intermediate removal hydrogen chloride production process, its energy consumption is greatly reduced by 80%, which is of great significance to energy conservation and emission reduction in this field.

[0030] As a preferred embodiment of the present invention, the discharge nozzle 15 is a fixed-angle spiral nozzle, and the refined gas and the mixed material are ejected through the discharge nozzle 15 and sprayed into the reactor in a fixed-angle inverted umbrella state to improve the efficiency of hydrogen chloride precipitation.

[0031] Furthermore, a mixing section 17 for material mixing is connected between the negative pressure section 18 and the diffusion section 16. The mixing section 17 extends along the direction of material flow to increase the mixing space and mixing time of the refined gas and the chloride intermediate to ensure sufficient separation of hydrogen chloride.

[0032] Furthermore, a reactor is provided, comprising a reactor body 12, a mounting hole is provided at the bottom of the reactor body 12, an inlet portion of a feed nozzle 21 is sealed and installed at the mounting hole, and preferably an annular flange is provided on the feed nozzle 21 of the mixing injector 11, and then the annular flange is sealed and docked with the mounting hole. The inlet of the feed nozzle 21 is connected in parallel with a chlorinated intermediate supply pipeline 2, a refined gas supply pipeline 1 and a chloride product discharge pipeline 10, and the top of the reactor body 12 is connected with a hydrogen chloride discharge pipeline 5. A discharge pipeline is connected between the bottom of the mass calibrator 3 and the reactor body 12, and a connecting valve is provided on the discharge pipeline, so that after the reaction is completed, the connecting valve is opened to discharge the material in the mass calibrator 3 into the reactor body 12. The chlorinated intermediate is introduced into the reactor body 12 through the chlorinated intermediate supply pipeline 2 via the feed nozzle 21, and then the refined gas is introduced into the reactor body 12 through the refined gas supply pipeline 1 via the feed nozzle 21 to precipitate hydrogen chloride gas. After the precipitation work is completed, the material after the removal of hydrogen chloride is collected through the chloride product discharge pipeline 10. Preferably, a material pump 9 is provided on the chloride product discharge pipeline 10 to extract the material after the removal of hydrogen chloride from the reactor body 12, and a chloride product collection mechanism 8 is provided at the discharge end of the chloride product discharge pipeline 10. Preferably, after the chlorinated intermediate is introduced into the reactor body 12, the material in the reactor body 12 reaches 80% of the volume of the reactor body 12, the chlorinated intermediate supply pipeline 2 is closed, the feeding is stopped, and the air pressure balance pipeline 4 is closed.

[0033] Preferably, a valve is provided on the refined gas supply pipeline 1 . In a specific operation process, the valve on the refined gas supply pipeline 1 is opened quantitatively according to actual needs to guide the refined gas into the reactor body 12 quantitatively.

[0034] As a preferred embodiment of the present invention, a vertically extending liquid level pipe 13 is provided on one side of the reactor body 12. The liquid level pipe 13 is opened at both ends. The bottom opening is connected in parallel with the chloride finished product discharge pipeline 10 to the inlet of the feed nozzle 21, and the top opening is connected in parallel with the chlorinated intermediate supply pipeline 2 and the refined gas supply pipeline 1, so that the chloride intermediate and the refined gas can enter the reactor body 12 from the liquid level pipe 13 and the feed nozzle 21, that is, through the same path to avoid dead corners where materials do not flow.

[0035] Furthermore, a mass calibrator 3 is connected in series to the chlorinated intermediate supply pipeline 2. In the specific process of removing hydrogen chloride, the chloride intermediate continuously enters the mass calibrator 3 through the chlorinated intermediate supply pipeline 2. In the process of introducing the chlorinated intermediate into the reactor body 12, the online mass calibration is completed. Preferably, the mass calibrator 3 has an inlet connected to the chlorinated intermediate supply pipeline 2 at the bottom and an outlet at the top to ensure that the chlorinated intermediate can fully fill the mass calibrator 3 and ensure the accuracy of the mass calibration.

[0036] Furthermore, the top structure of the reactor body 12 is conical, and its radial cross section gradually decreases from bottom to top, and the hydrogen chloride discharge pipeline 5 is connected to the top position of the reactor body 12. The sucked hydrogen chloride gas is made to conform to the rising law of hot gas in the discharge route, avoiding uneven pressure inside the reactor body 12 and affecting the removal speed of hydrogen chloride.

[0037] Preferably, the hydrogen chloride discharge pipeline 5 is connected to a gas-liquid separator 6, the liquid discharge port of the gas-liquid separator 6 is connected to the reactor body 12, and the gas discharge port of the gas-liquid separator 6 is connected to a hydrogen chloride gas collection mechanism, the precipitated hydrogen chloride is purified by the gas-liquid separator 6, the chloride intermediates carried out by the hydrogen chloride gas are intercepted and refluxed to the reactor body 12, and the separated hydrogen chloride gas is fully absorbed. A stabilizer inlet 7 is provided on the connecting pipeline between the liquid discharge port and the reactor body 12.

[0038] Furthermore, the top of the reactor body 12 is connected to a pressure balance pipeline 4 which is distributed in parallel with the hydrogen chloride discharge pipeline 5, and the gas outlet of the pressure balance pipeline 4 is connected to a chlorination reactor. In the process of introducing the chlorinated intermediate into the reactor, the chlorinated intermediate is surged through the discharge nozzle 15 and the through hole 19, and the precipitated gas of the chlorinated intermediate is discharged from the top of the reactor through the pressure balance pipeline 4 and introduced into the chlorination reactor, so as to achieve the purpose of pressure balance. It also creates conditions for continuous chlorination production, and at the same time omits the feed pump of the chloride intermediate.

[0039] Preferably, a sampling point 14 is provided on the reactor body 12. During the process of blowing off hydrogen chloride from the chloride intermediate, the sampling point 14 detects the hydrogen chloride content at a set time, and stops blowing off after reaching the standard. The chloride finished product discharge pipeline 10 is opened, and the material after the hydrogen chloride is removed is pumped out of the reactor body 12 through the material pump 9. Preferably, a chloride finished product collecting mechanism 8 is provided at the discharge end of the chloride finished product discharge pipeline 10 to package the chloride finished product.

[0040] A removal method is also provided, comprising the following steps:

[0041] Online mass calibration: The chloride intermediate continuously enters the mass calibrator 3 through the inlet of the chlorinated intermediate supply pipeline 2 to complete the online mass calibration;

[0042] Passing chloride intermediate: After completing the online mass calibration, the chloride intermediate continuously enters the feed nozzle 21 connected to the reactor body 12 through the liquid level pipe 13, and enters the reactor body 12 through the discharge nozzle 15 and the through hole 19 on the connecting section 20. The gas precipitated from the surging chloride intermediate returns to the chlorination reactor from the air pressure balance pipe 4, and forms an air pressure balance in a connected state with the chlorination reactor;

[0043] Preparation before introducing the refined gas: After the material in the reactor body 12 reaches 80% of the reactor volume, close the chlorinated intermediate supply pipeline 2, close the gas pressure balance pipeline 4, and close the liquid discharge port of the gas-liquid separator 6;

[0044] Introducing refined gas: Open the refined gas supply pipeline 1, guide the refined gas from the feed nozzle 21 into the reactor body 12, the refined gas flows through the negative pressure section 18, and generates negative pressure at the negative pressure section 18, and the chlorinated intermediate in the reactor body 12 is reversely sucked into the negative pressure section 18 from the through hole 19 of the connecting section 20, and the chlorinated intermediate and the refined gas are mixed in the negative pressure section 18 and the mixing section 17. During the mixing process, the saturated hydrogen chloride gas in the chlorinated intermediate is precipitated and ejected from the discharge nozzle 15 together with the chlorinated intermediate and the refined gas, the saturated hydrogen chloride gas and the refined gas float up and flow into the hydrogen chloride discharge pipeline 5, and are discharged into the hydrogen chloride gas collection mechanism after being purified by the gas-liquid separator 6.

[0045] Adaptive changes made according to actual needs are all within the protection scope of the present invention.

[0046] It should be noted that it is obvious to those skilled in the art that the present invention is not limited to the details of the exemplary embodiments described above, and that the present invention can be implemented in other specific forms without departing from the spirit or essential features of the present invention. Therefore, the embodiments should be regarded as exemplary and non-restrictive from any point of view, and the scope of the present invention is defined by the appended claims rather than the above description, and it is intended that all changes falling within the meaning and scope of the equivalent elements of the claims are included in the present invention. Any reference numerals in the claims should not be regarded as limiting the claims involved.

[0047] The present invention uses specific examples to illustrate the principles and implementation methods of the present invention. The above examples are only used to help understand the method and core ideas of the present invention. At the same time, for those skilled in the art, according to the ideas of the present invention, there will be changes in the specific implementation methods and application scope. In summary, the content of this specification should not be understood as limiting the present invention.

Claims

1. A method for removing hydrogen chloride phase, characterized in that: The equipment for removing the hydrogen chloride phase comprises a reactor and a mixing ejector, wherein the mixing ejector comprises a feed nozzle, a suction sleeve and a discharge nozzle, which are all installed in the reactor and arranged in sequence along the material flow direction, the flow cross section of the feed nozzle gradually decreases along the material flow direction, and the inlet of the feed nozzle is connected with a feed pipe located outside the reactor, the suction sleeve is divided into a connecting section, a negative pressure section and a diffusion section in sequence along the material flow direction, the connecting section is coaxially sleeved at the outlet of the feed nozzle, a plurality of through holes connected to the inside of the reactor are opened on the connecting section, and each of the through holes surrounds the outer peripheral side of the outlet of the feed nozzle at equal intervals along the circumferential direction, the flow cross section of the negative pressure section gradually decreases along the material flow direction, the flow cross section of the diffusion section gradually increases in the opposite direction of the material flow, and the discharge nozzle is connected at the outlet of the diffusion section; The reactor comprises a reactor body, a mounting hole is provided at the bottom of the reactor body, an inlet portion of the feed nozzle is sealed and installed at the mounting hole, a chlorinated intermediate supply pipeline, a refined gas supply pipeline and a chloride product discharge pipeline are connected in parallel to the inlet of the feed nozzle, and a hydrogen chloride discharge pipeline is connected to the top of the reactor body; The removal method for removing the hydrogen chloride phase comprises the following steps: Online mass calibration: The chloride intermediate continuously enters the mass calibrator through the inlet of the chlorinated intermediate supply pipeline to complete the online mass calibration; Passing in the chloride intermediate: after completing the online mass calibration, the chloride intermediate continuously enters the feed nozzle connected to the reactor body through the liquid level pipeline, and enters the reactor body through the discharge nozzle and the through hole on the connecting section, and the gas precipitated from the chloride intermediate is returned to the chlorination reactor from the air pressure balance pipeline, forming an air pressure balance in a connected state with the chlorination reactor; Preparation before introducing refined gas: after the material in the reactor body reaches 80% of the reactor volume, close the chlorinated intermediate supply pipeline, close the gas pressure balance pipeline, and close the liquid outlet of the gas-liquid separator; Introducing refined gas: opening the refined gas supply pipeline, guiding the refined gas from the feed nozzle into the reactor body, the refined gas flows through the negative pressure section, and generates negative pressure at the negative pressure section, and the chlorinated intermediate in the reactor body is reversely sucked into the negative pressure section from the through hole of the connecting section, and the chlorinated intermediate is mixed with the refined gas in the negative pressure section and the mixing section. During the mixing process, the saturated hydrogen chloride gas in the chlorinated intermediate is precipitated and ejected from the discharge nozzle together with the chlorinated intermediate and the refined gas, the saturated hydrogen chloride gas and the refined gas float up and flow into the hydrogen chloride discharge pipeline, and are discharged into the hydrogen chloride gas collection mechanism after being purified by the gas-liquid separator.

2. The method for removing the hydrogen chloride phase according to claim 1, characterized in that: The discharge nozzle is a fixed-angle spiral nozzle.

3. The method for removing the hydrogen chloride phase according to claim 2, characterized in that: A mixing section for mixing materials is connected between the negative pressure section and the diffusion section, and the mixing section extends along the direction of material flow.

4. The method for removing the hydrogen chloride phase according to claim 3, characterized in that: A vertically extending liquid level pipeline is provided on one side of the reactor body. Both ends of the liquid level pipeline are open. The bottom opening is connected in parallel with the chloride product discharge pipeline to the inlet of the feed nozzle, and the top opening is connected in parallel with the chlorinated intermediate supply pipeline and the refined gas supply pipeline.

5. The method for removing the hydrogen chloride phase according to claim 4, characterized in that: A mass calibrator is connected in series on the chlorinated intermediate supply pipeline.

6. The method for removing hydrogen chloride phase according to claim 5, characterized in that: The top structure of the reactor body is conical, and its radial cross section gradually decreases from bottom to top. The hydrogen chloride discharge pipeline is connected to the top position of the reactor body.

7. The method for removing the hydrogen chloride phase according to claim 6, characterized in that: The hydrogen chloride discharge pipeline is connected to a gas-liquid separator, the liquid discharge port of the gas-liquid separator is connected to the reactor body, and the gas discharge port of the gas-liquid separator is connected to a hydrogen chloride gas collecting mechanism.

8. The method for removing hydrogen chloride phase according to claim 7, characterized in that: The top of the reactor body is connected to a gas pressure balance pipeline which is distributed in parallel with the hydrogen chloride discharge pipeline, and the gas outlet of the gas pressure balance pipeline is connected to a chlorination reactor.

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