Gas-liquid reaction system and gas-liquid reaction method

Abstract

The invention provides a gas-liquid reaction system and a gas-liquid reaction method, aiming at the gas-liquid reaction system, continuous reaction of a liquid-phase raw material and a gas-phase raw material is realized through a plurality of groups of gas-liquid reactors and gas-liquid separators, complete reaction of liquid-phase raw materials is achieved through the first gas-liquid reactor, recovery of excessive gas-phase raw materials and collection of liquid-phase products generated by the first gas-liquid reactor are achieved through the first gas-liquid separator, complete reaction of the excessive gas-phase raw materials is achieved through the second gas-liquid reactor, and recovery of excessive liquid-phase raw materials is achieved through the second gas-liquid separator. The third gas-liquid reactor realizes complete reaction of excessive liquid-phase raw materials, and the first gas-liquid separator also realizes collection of liquid-phase products generated by the second gas-liquid reactor and the third gas-liquid reactor, that is, in the continuous reaction process, on one hand, full reaction of the gas-phase raw materials and the liquid-phase raw materials is realized, so that the product quality is ensured, and the production cost is reduced; on the other hand, the maximum utilization of the liquid-phase raw material and the gas-phase raw material is realized, so that the production cost is saved.

Description

Technical Field

[0001] The present application relates to the field of gas-liquid reaction, and in particular, to a gas-liquid reaction system and a gas-liquid reaction method. Background Art

[0002] The gas-liquid reaction system is a reaction system widely used in the fields of chemical industry, energy, environment and biochemistry, that is, gas-phase raw materials and liquid-phase raw materials generate corresponding products through gas-liquid reaction. In industrial production, gas-liquid reactions mostly use reaction tanks as the main equipment, which require manual feeding, and the reaction process is difficult to achieve continuous. At the same time, when the product is also in liquid phase, the incompletely reacted liquid-phase raw materials will enter the liquid-phase product as impurities, thereby affecting the product quality. Summary of the invention

[0003] The present application at least provides a gas-liquid reaction system and a gas-liquid reaction method. For the above-mentioned gas-liquid reaction system, a continuous reaction of liquid raw materials and gas raw materials is achieved through multiple groups of gas-liquid reactors and gas-liquid separators. During the continuous reaction process, on the one hand, a full reaction of the gas raw materials and the liquid raw materials is achieved, and the product quality is ensured by avoiding the mixing of the liquid raw materials and the liquid products. On the other hand, the maximum utilization of the liquid raw materials and the gas raw materials is achieved, thereby saving production costs.

[0004] The present application provides a gas-liquid reaction system, which includes a liquid phase feeding system, a gas phase feeding system, a first ejector, a first gas-liquid reactor, a first gas-liquid separator, a second ejector, a second gas-liquid reactor, a second gas-liquid separator, a third ejector, and a third gas-liquid reactor:

[0005] The liquid phase feeding system is connected to the continuous phase main line of the first ejector and the continuous phase main line of the second ejector respectively;

[0006] The gas phase feeding system is connected to the discrete phase side pipeline of the first ejector, the discrete phase side pipeline of the third ejector, the gas supply port of the first gas-liquid reactor, and the gas supply port of the third gas-liquid reactor respectively;

[0007] The outlet of the first ejector is connected to the inlet of the first gas-liquid reactor, and the outlet of the first gas-liquid reactor is connected to the inlet of the first gas-liquid separator; the first ejector is used to mix the liquid raw material provided by the liquid feeding system with the gas raw material provided by the gas feeding system, and the first gas-liquid reactor is used to carry out a gas-liquid reaction between the liquid raw material and the gas raw material to obtain a liquid product, wherein the gas replenishing port of the first gas-liquid reactor is used to provide excess gas raw material to ensure that the liquid raw material in the first gas-liquid reactor is fully reacted, and the first gas-liquid separator is used to achieve gas-liquid separation between the liquid product of the first gas-liquid reactor and the gas raw material that has not reacted completely;

[0008] The gas phase outlet of the first gas-liquid separator is connected to the discrete phase side pipeline of the second ejector, the outlet of the second ejector is connected to the inlet of the second gas-liquid reactor, and the outlet of the second gas-liquid reactor is connected to the inlet of the second gas-liquid separator; the second ejector is used to mix the liquid phase raw material provided by the liquid phase feeding system with the gas phase raw material separated by the first gas-liquid separator, and the second gas-liquid reactor is used to carry out gas-liquid reaction between the liquid phase raw material and the gas phase raw material separated by the first gas-liquid separator to obtain a liquid phase product, wherein the excess liquid phase raw material in the second gas-liquid reactor is used to ensure that the gas phase raw material in the second gas-liquid reactor is fully reacted, and the second gas-liquid separator is used to separate the liquid phase product of the second gas-liquid reactor and the liquid phase raw material that has not reacted completely from the residual gas phase components;

[0009] The liquid phase outlet of the second gas-liquid separator is connected to the continuous phase main pipeline of the third ejector, the outlet of the third ejector is connected to the inlet of the third gas-liquid reactor, and the outlet of the third gas-liquid reactor is connected to the inlet of the first gas-liquid separator; the third ejector is used to mix the liquid phase product of the second gas-liquid reactor and the liquid phase raw material that has not reacted completely with the gas phase raw material provided by the gas phase feeding system, and the third gas-liquid reactor is used to carry out gas-liquid reaction between the liquid phase raw material that has not reacted completely in the second gas-liquid reactor and the gas phase raw material provided by the gas phase feeding system to obtain a liquid phase product, wherein the gas replenishment port of the third gas-liquid reactor is used to provide excess gas phase raw material to ensure that the liquid phase raw material in the third gas-liquid reactor is fully reacted, and the first gas-liquid separator is also used to achieve gas-liquid separation between the liquid phase product of the second gas-liquid reactor and the liquid phase product of the third gas-liquid reactor and the gas phase raw material that has not reacted completely.

[0010] The present application also provides a gas-liquid reaction method, which comprises:

[0011] The liquid phase feeding system continuously delivers liquid phase raw materials to the continuous phase main pipeline of the first ejector, and the gas phase feeding system continuously delivers gas phase raw materials to the discrete phase side pipeline of the first ejector synchronously;

[0012] Mixing the liquid raw material provided by the liquid feeding system with the gas raw material provided by the gas feeding system through the first ejector, and conveying the mixed fluid to the first gas-liquid reactor;

[0013] A first gas-liquid reactor is used to carry out a gas-liquid reaction between a liquid-phase raw material and a gas-phase raw material to obtain a liquid-phase product, wherein an excess of the gas-phase raw material is provided through a gas supply port of the first gas-liquid reactor to ensure that the liquid-phase raw material in the first gas-liquid reactor is fully reacted;

[0014] The fluid after the reaction in the first gas-liquid reactor is transported to the first gas-liquid separator, and the first gas-liquid separator is used to separate the liquid phase product of the first gas-liquid reactor from the gas phase raw material that has not reacted completely;

[0015] The liquid phase product separated by the first gas-liquid separator is collected, and the gas phase raw material separated by the first gas-liquid separator is transported to the discrete phase side pipeline of the second ejector, and the liquid phase feeding system simultaneously continuously transports the liquid phase raw material to the continuous phase main pipeline of the second ejector;

[0016] Mixing the liquid phase raw material provided by the liquid phase feeding system with the gas phase raw material separated by the first gas-liquid separator through the second ejector, and conveying the mixed fluid to the second gas-liquid reactor;

[0017] The liquid raw material and the gas raw material separated by the first gas-liquid separator are subjected to a gas-liquid reaction in a second gas-liquid reactor to obtain a liquid product, wherein an excess of liquid raw material is provided to the second gas-liquid reactor to ensure that the gas raw material in the second gas-liquid reactor is fully reacted;

[0018] The fluid after the reaction in the second gas-liquid reactor is transported to the second gas-liquid separator, and the second gas-liquid separator is used to separate the liquid phase product of the second gas-liquid reactor from the liquid phase raw material that has not reacted completely and the residual gas phase components;

[0019] The liquid phase product separated by the second gas-liquid separator and the incompletely reacted liquid phase raw material are transported to the continuous phase main pipeline of the third ejector, and the gas phase feeding system simultaneously continuously transports the gas phase raw material to the discrete phase side pipeline of the third ejector;

[0020] The liquid phase product and the incompletely reacted liquid phase raw material of the second gas-liquid reactor are mixed with the gas phase raw material provided by the gas phase feeding system through the third ejector, and the mixed fluid is transported to the third gas-liquid reactor;

[0021] The unreacted liquid raw material and the gas raw material are subjected to a gas-liquid reaction by a third gas-liquid reactor to obtain a liquid product, wherein an excess of the gas raw material is provided through a gas supply port of the third gas-liquid reactor to ensure that the liquid raw material in the third gas-liquid reactor is fully reacted;

[0022] The fluid after the reaction in the third gas-liquid reactor is transported to the first gas-liquid separator, and the first gas-liquid separator is used to achieve gas-liquid separation between the liquid products of the second gas-liquid reactor and the liquid products of the third gas-liquid reactor and the incompletely reacted gas-phase raw materials, so that the incompletely reacted gas-phase raw materials can be subjected to gas-liquid reaction again through the second ejector, the second gas-liquid reactor, the second gas-liquid separator, the third ejector and the third gas-liquid reactor.

[0023] In summary, the present application provides a gas-liquid reaction system and a gas-liquid reaction method, the system comprising a liquid-phase feeding system, a gas-phase feeding system, a first ejector, a first gas-liquid reactor, a first gas-liquid separator, a second ejector, a second gas-liquid reactor, a second gas-liquid separator, a third ejector, and a third gas-liquid reactor: the liquid-phase feeding system is respectively connected to the continuous phase main line of the first ejector and the continuous phase main line of the second ejector; the gas-phase feeding system is respectively connected to the discrete phase side pipeline of the first ejector, the discrete phase side pipeline of the third ejector, the gas supply port of the first gas-liquid reactor, and the gas supply port of the third gas-liquid reactor; the outlet of the first ejector is connected to the inlet of the first gas-liquid reactor, and the first gas-liquid reactor The outlet of the first gas-liquid separator is connected to the inlet of the first gas-liquid separator; the first ejector is used to mix the liquid raw material provided by the liquid feeding system with the gas raw material provided by the gas feeding system, and the first gas-liquid reactor is used for the liquid raw material and the gas raw material to carry out a gas-liquid reaction to obtain a liquid product, wherein the gas replenishing port of the first gas-liquid reactor is used to provide an excess of gas raw material to ensure that the liquid raw material in the first gas-liquid reactor is fully reacted, and the first gas-liquid separator is used to achieve gas-liquid separation between the liquid product of the first gas-liquid reactor and the gas raw material that has not reacted completely; the gas phase outlet of the first gas-liquid separator is connected to the discrete phase side pipeline of the second ejector, the outlet of the second ejector is connected to the inlet of the second gas-liquid reactor, and the second gas-liquid reactor The outlet of the second gas-liquid separator is connected to the inlet of the second gas-liquid separator; the second ejector is used to mix the liquid raw material provided by the liquid feeding system with the gas raw material separated by the first gas-liquid separator, and the second gas-liquid reactor is used to carry out gas-liquid reaction between the liquid raw material and the gas raw material separated by the first gas-liquid separator to obtain a liquid product, wherein the excess liquid raw material in the second gas-liquid reactor is used to ensure that the gas raw material in the second gas-liquid reactor is fully reacted, and the second gas-liquid separator is used to separate the liquid product of the second gas-liquid reactor and the liquid raw material that has not reacted completely from the residual gas components; the liquid phase outlet of the second gas-liquid separator is connected to the continuous phase main pipeline of the third ejector, and the outlet of the third ejector is connected to the inlet of the third gas-liquid reactor. The outlet of the third gas-liquid reactor is connected to the inlet of the first gas-liquid separator; the third ejector is used to mix the liquid product of the second gas-liquid reactor and the liquid raw material that has not reacted completely with the gas raw material provided by the gas feeding system; the third gas-liquid reactor is used to carry out gas-liquid reaction between the liquid raw material that has not reacted completely in the second gas-liquid reactor and the gas raw material provided by the gas feeding system to obtain a liquid product, wherein the gas replenishing port of the third gas-liquid reactor is used to provide excess gas raw material to ensure that the liquid raw material in the third gas-liquid reactor is fully reacted, and the first gas-liquid separator is also used to achieve gas-liquid separation between the liquid product of the second gas-liquid reactor and the liquid product of the third gas-liquid reactor and the gas raw material that has not reacted completely.For the above-mentioned gas-liquid reaction system, a continuous reaction of liquid-phase raw materials and gas-phase raw materials is achieved through multiple groups of gas-liquid reactors and gas-liquid separators, wherein the first gas-liquid reactor is used to complete the reaction of the liquid-phase raw materials, the first gas-liquid separator is used to recover the excess gas-phase raw materials and collect the liquid-phase products produced by the first gas-liquid reactor, the second gas-liquid reactor is used to complete the reaction of the excess gas-phase raw materials, the second gas-liquid separator is used to recover the excess liquid-phase raw materials, the third gas-liquid reactor is used to complete the reaction of the excess liquid-phase raw materials, and the first gas-liquid separator is used to collect the liquid-phase products produced by the second gas-liquid reactor and the third gas-liquid reactor. That is, in the continuous reaction process, on the one hand, the gas-phase raw materials and the liquid-phase raw materials are fully reacted, and the product quality is guaranteed by avoiding the mixing of the liquid-phase raw materials and the liquid-phase products. On the other hand, the maximum utilization of the liquid-phase raw materials and the gas-phase raw materials is achieved, thereby saving production costs.

[0024] Other advantages of the present application will be explained in more detail in conjunction with the following description and drawings.

[0025] It should be understood that the above description is only an overview of the technical solution of the present application, so that the technical means of the present application can be generally understood and then implemented according to the contents of the specification. In order to make the above and other purposes, features and advantages of the present application more obvious and easy to understand, the specific implementation methods of the present application are specifically described below by way of example. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] In order to more clearly illustrate the technical solutions of the embodiments of the present application, the following is a brief introduction to the drawings required for use in the embodiments. The drawings herein are incorporated into the specification and constitute a part of the specification. These drawings illustrate embodiments that conform to the present application and are used together with the specification to illustrate the technical solutions of the present application. It should be understood that the drawings only illustrate certain embodiments of the present application and should not be regarded as limiting the scope of protection. For ordinary technicians in this field, other relevant drawings can be obtained based on these drawings without creative work. Moreover, the same reference numerals are used to represent the same components throughout the drawings. In the drawings:

[0027] Figure 1 A schematic diagram of the structure of a gas-liquid reaction system provided in an embodiment of the present application;

[0028] Figure 2 A schematic structural diagram of a first gas-liquid reactor provided in an embodiment of the present application;

[0029] In the drawings, the same or corresponding reference numerals represent the same or corresponding parts.

[0030] Among them, 100-liquid phase feeding system; 1-first dissolving tank; 2-first metering pump; 3-second dissolving tank; 4-second metering pump; 200-gas phase feeding system; 5-liquid-solid reactor; 6-gas buffer tank; 7-first ejector; 8-first gas-liquid reactor; 81-gas supply pipeline; 82-static mixing plug-in; 83-series structure; 9-first gas-liquid separator; 10-second ejector; 11-second gas-liquid reactor; 12-second gas-liquid separator; 13-third ejector; 14-third gas-liquid reactor. DETAILED DESCRIPTION

[0031] The exemplary embodiments of the present application will be described in more detail below with reference to the accompanying drawings. Although the exemplary embodiments of the present application are shown in the accompanying drawings, it should be understood that the present application can be implemented in various forms and should not be limited by the embodiments described herein. On the contrary, these embodiments are provided to enable a more thorough understanding of the present application and to fully convey the scope of the present application to those skilled in the art.

[0032] In the description of the embodiments of the present application, it should be understood that terms such as "including" or "having" are intended to indicate the presence of the disclosed features, numbers, components, parts or a combination thereof in the present specification, and do not exclude the possibility of the presence of one or more other features, numbers, components, parts or a combination thereof.

[0033] Unless otherwise specified, “ / ” means or. For example, A / B can mean A or B. The “and / or” in this article is merely a way to describe the association relationship of associated objects, indicating that three relationships can exist. For example, A and / or B can mean: A exists alone, A and B exist at the same time, and B exists alone.

[0034] The terms "first", "second", etc. are used only to distinguish the same or similar technical features for the convenience of description, and should not be understood as indicating or implying the relative importance or quantity of these technical features. Thus, the features defined by "first", "second", etc. may explicitly or implicitly include one or more of such features. In the description of the embodiments of the present application, unless otherwise specified, the term "plurality" means two or more than two.

[0035] In industrial production, gas-liquid reactions mostly use reaction tanks as the main equipment, which requires manual feeding, and the reaction process is difficult to achieve continuity. At the same time, when the product is also in liquid phase, the incompletely reacted liquid raw materials will enter the liquid product in the form of impurities, thereby affecting the product quality.

[0036] In view of this, the present application provides a gas-liquid reaction system and a gas-liquid reaction method. For the above-mentioned gas-liquid reaction system, a continuous reaction of liquid raw materials and gas raw materials is realized through multiple groups of gas-liquid reactors and gas-liquid separators. During the continuous reaction process, on the one hand, a full reaction of the gas raw materials and the liquid raw materials is achieved, and the product quality is ensured by avoiding the mixing of the liquid raw materials and the liquid products. On the other hand, the maximum utilization of the liquid raw materials and the gas raw materials is achieved, thereby saving production costs.

[0037] The present application will be described in detail below with reference to the accompanying drawings and in combination with embodiments.

[0038] like Figure 1 As shown, the present application provides a gas-liquid reaction system, characterized in that the system includes a liquid phase feeding system 100, a gas phase feeding system 200, a first ejector 7, a first gas-liquid reactor 8, a first gas-liquid separator 9, a second ejector 10, a second gas-liquid reactor 11, a second gas-liquid separator 12, a third ejector 13, and a third gas-liquid reactor 14:

[0039] The liquid phase feeding system 100 is connected to the continuous phase main line of the first ejector 7 and the continuous phase main line of the second ejector 10 respectively.

[0040] Specifically, the liquid-phase feeding system 100 is used to realize the continuous delivery of liquid-phase raw materials.

[0041] It should be noted that, in the present embodiment, in order to facilitate the subsequent reaction of the liquid-phase raw material and the gas-phase raw material, the liquid-phase raw material and the gas-phase raw material are mixed through an ejector. The ejector is a device that utilizes a high-pressure fluid (such as gas or liquid) to spray through a nozzle to create a low-pressure area, thereby sucking in the low-pressure fluid and mixing with it. The first ejector 7, the second ejector 10, and the third ejector 13 can adopt the same structure.

[0042] The gas phase feeding system 200 is connected to the discrete phase side pipeline of the first ejector 7, the discrete phase side pipeline of the third ejector 13, the gas supply port of the first gas-liquid reactor 8, and the gas supply port of the third gas-liquid reactor 14 respectively.

[0043] Specifically, the gas-phase feeding system 200 is used to realize the continuous transportation of gas-phase raw materials.

[0044] It should be noted that, in this embodiment, the gas-liquid reaction of the gas-phase raw material and the liquid-phase raw material is achieved through a gas-liquid reactor, and the first gas-liquid reactor 8, the second gas-liquid reactor 11, and the third gas-liquid reactor 14 can adopt the same structure.

[0045] Considering that when the product is also in liquid phase, the incompletely reacted liquid phase raw material will enter the liquid phase product, and the raw material and product that are both in liquid phase will be difficult to separate, resulting in the liquid phase raw material existing in the form of impurities, thereby affecting the product quality. In this regard, in this embodiment, the gas replenishment ports of the first gas-liquid reactor 8 and the third gas-liquid reactor 14 can be connected to the gas phase feeding system 200, so that the excess gas phase raw material can be used later to ensure the complete reaction of the liquid phase raw material.

[0046] The outlet of the first ejector 7 is connected to the inlet of the first gas-liquid reactor 8, and the outlet of the first gas-liquid reactor 8 is connected to the inlet of the first gas-liquid separator 9; the first ejector 7 is used to mix the liquid raw material provided by the liquid feeding system 100 with the gas raw material provided by the gas feeding system 200, and the first gas-liquid reactor 8 is used for the liquid raw material and the gas raw material to carry out a gas-liquid reaction to obtain a liquid product, wherein the gas replenishing port of the first gas-liquid reactor 8 is used to provide excess gas raw material to ensure that the liquid raw material in the first gas-liquid reactor 8 is fully reacted, and the first gas-liquid separator 9 is used to achieve gas-liquid separation between the liquid product of the first gas-liquid reactor 8 and the gas raw material that has not reacted completely.

[0047] Specifically, the gas-phase raw material and the liquid-phase raw material are mixed by the first ejector 7, the liquid-phase raw material is fully reacted by the excess gas-phase raw material in the first gas-liquid reactor 8, and the liquid-phase product and the excess gas-phase raw material of the first gas-liquid reactor 8 are collected separately by the first gas-liquid separator 9.

[0048] The gas phase outlet of the first gas-liquid separator 9 is connected to the discrete phase side pipeline of the second ejector 10, the outlet of the second ejector 10 is connected to the inlet of the second gas-liquid reactor 11, and the outlet of the second gas-liquid reactor 11 is connected to the inlet of the second gas-liquid separator 12; the second ejector 10 is used to mix the liquid phase raw material provided by the liquid phase feeding system 100 with the gas phase raw material separated by the first gas-liquid separator 9, and the second gas-liquid reactor 11 is used for the liquid phase raw material and the gas phase raw material separated by the first gas-liquid separator 9 to carry out gas-liquid reaction to obtain a liquid phase product, wherein the excess liquid phase raw material in the second gas-liquid reactor 11 is used to ensure that the gas phase raw material in the second gas-liquid reactor 11 is fully reacted, and the second gas-liquid separator 12 is used to separate the liquid phase product of the second gas-liquid reactor 11 and the liquid phase raw material that has not reacted completely from the residual gas phase components to achieve gas-liquid separation.

[0049] Specifically, the liquid phase product of the first gas-liquid reactor 8 can be collected through the liquid phase outlet of the first gas-liquid separator 9, the excess gas phase raw material of the first gas-liquid reactor 8 can be collected through the gas phase outlet of the first gas-liquid separator 9, the excess gas phase raw material and the liquid phase raw material are mixed through the second ejector 10, the excess liquid phase raw material in the second gas-liquid reactor 11 is used to achieve full reaction of the gas phase raw material, and the liquid phase product of the second gas-liquid reactor 11, the incompletely reacted liquid phase raw material, and the residual gas phase components are collected separately through the second gas-liquid separator 12.

[0050] It should be noted that the excess liquid raw material in the second gas-liquid reactor 11 can achieve sufficient reaction of the gas raw material, but in actual applications, the gas raw material is usually a mixed gas, and the second gas-liquid separator 12 can collect the residual gas components. The residual gas components are the remaining gas components that do not participate in the reaction. For this, tail gas treatment can be carried out directly.

[0051] The liquid phase outlet of the second gas-liquid separator 12 is connected to the continuous phase main line of the third ejector 13, the outlet of the third ejector 13 is connected to the inlet of the third gas-liquid reactor 14, and the outlet of the third gas-liquid reactor 14 is connected to the inlet of the first gas-liquid separator 9; the third ejector 13 is used to mix the liquid phase product of the second gas-liquid reactor 11 and the liquid phase raw material that has not reacted completely with the gas phase raw material provided by the gas phase feeding system 200, and the third gas-liquid reactor 14 is used to carry out gas-liquid reaction between the liquid phase raw material that has not reacted completely in the second gas-liquid reactor 11 and the gas phase raw material provided by the gas phase feeding system 200 to obtain a liquid phase product, wherein the gas replenishment port of the third gas-liquid reactor 14 is used to provide excess gas phase raw material to ensure that the liquid phase raw material in the third gas-liquid reactor 14 is fully reacted, and the first gas-liquid separator 9 is also used to achieve gas-liquid separation between the liquid phase product of the second gas-liquid reactor 11 and the liquid phase product of the third gas-liquid reactor 14 and the gas phase raw material that has not reacted completely.

[0052] Specifically, the liquid phase product and the incompletely reacted liquid phase raw material of the second gas-liquid reactor 11 can be collected through the liquid phase outlet of the second gas-liquid separator 12, and the liquid phase product, the incompletely reacted liquid phase raw material and the gas phase raw material of the second gas-liquid reactor 11 can be mixed through the third ejector 13. The excess gas phase raw material in the third gas-liquid reactor 14 can be used to fully react the liquid phase raw material. Then, the liquid phase product of the second gas-liquid reactor 11 and the liquid phase product of the third gas-liquid reactor 14 and the excess gas phase raw material can be collected separately through the first gas-liquid separator 9. At this time, the gas phase outlet of the first gas-liquid separator 9 can collect the excess gas phase raw material of the third gas-liquid reactor 14 so that the second gas-liquid reactor 11 can fully react with the excess gas phase raw material.

[0053] It can be seen that the gas-liquid reaction system realizes the continuous reaction of liquid raw materials and gas raw materials through multiple groups of gas-liquid reactors and gas-liquid separators, wherein the first gas-liquid reactor 8 realizes the complete reaction of the liquid raw material, the first gas-liquid separator 9 realizes the recovery of excess gas raw materials and the collection of liquid products produced by the first gas-liquid reactor 8, the second gas-liquid reactor 11 realizes the complete reaction of excess gas raw materials, the second gas-liquid separator 12 realizes the recovery of excess liquid raw materials, the third gas-liquid reactor 14 realizes the complete reaction of excess liquid raw materials, and the first gas-liquid separator 9 also realizes the collection of liquid products produced by the second gas-liquid reactor 11 and the third gas-liquid reactor 14. That is, in the continuous reaction process, on the one hand, the gas raw materials and the liquid raw materials are fully reacted, and the product quality is guaranteed by avoiding the mixing of the liquid raw materials and the liquid products. On the other hand, the maximum utilization of the liquid raw materials and the gas raw materials is realized, thereby saving production costs.

[0054] In a possible implementation, the first gas-liquid reactor 8 includes a plurality of reaction pipelines and a plurality of series structures 83 . The plurality of reaction pipelines are arranged in parallel, and the series structure 83 is used to connect two adjacent reaction pipelines.

[0055] Specifically, Figure 2 As shown, multiple reaction pipelines are arranged in parallel inside the first gas-liquid reactor 8 and connected by a series structure 83, so that the internal fluid can flow in series through the multiple reaction pipelines from the inlet to the outlet of the first gas-liquid reactor 8. The structural design of multiple reaction pipelines and multiple series structures 83 realizes a compact design of long series pipelines, which saves space while ensuring the length of the reaction pipelines.

[0056] In a possible implementation, the first gas-liquid reactor 8 further includes a plurality of static mixing plug-ins 82 , which are distributed in a plurality of reaction pipelines, and the static mixing plug-ins 82 have cutting surfaces.

[0057] Specifically, Figure 2 As shown, a static mixing plug-in 82 can be arranged inside the first gas-liquid reactor 8. Since the static mixing plug-in 82 has a cutting surface, the static mixing plug-in 82 can cut and break the bubbles, so that the gas-phase raw materials can exist in the form of tiny bubbles to ensure the mixing uniformity of the gas-liquid two-phases in the flow process of the reaction pipeline. At the same time, the gas-liquid interface can be continuously updated to accelerate the reaction rate. At the same time, the presence of the static mixing plug-in 82 can increase the turbulence intensity in the reaction pipeline, enhance the heat exchange efficiency from the center of the reaction pipeline to the outer wall of the pipeline, and improve the uniformity of the temperature distribution in the reaction pipeline. For strong exothermic reactions, the reaction heat can be removed in time to avoid local overheating or even temperature runaway that may occur in the kettle equipment, thereby improving the safety of the reaction process.

[0058] In a possible implementation, the first gas-liquid reactor 8 further includes a gas supply pipeline 81, and an outlet of the gas supply pipeline 81 is arranged inside any reaction pipeline among the multiple reaction pipelines.

[0059] Specifically, Figure 2 As shown, in order to facilitate the provision of excess gas-phase raw materials to the first gas-liquid reactor 8, a gas supplement pipeline 81 may also be included in the first gas-liquid reactor 8.

[0060] In a possible implementation, a heat exchange jacket is provided outside the first gas-liquid reactor 8 to remove the reaction heat in a timely manner.

[0061] It should be noted that, in this embodiment, the second gas-liquid reactor 11 and the third gas-liquid reactor 14 may have the same structure as the first gas-liquid reactor 8 .

[0062] In a possible implementation, the liquid phase feeding system 100 includes a first dissolving tank 1, a first metering pump 2, a second dissolving tank 3, and a second metering pump 4:

[0063] The outlet of the first dissolving tank 1 is connected to the inlet of the first metering pump 2, and the outlet of the first metering pump 2 is connected to the continuous phase main line of the first ejector 7; the first dissolving tank 1 is used to dissolve the liquid raw material, and the first metering pump 2 is used for quantitative delivery of the liquid raw material;

[0064] The outlet of the second dissolving tank 3 is connected to the inlet of the second metering pump 4, and the outlet of the second metering pump 4 is connected to the continuous phase main pipeline of the second ejector 10; the second dissolving tank 3 is used to dissolve the liquid raw material, and the second metering pump 4 is used for quantitative transportation of the liquid raw material.

[0065] Specifically, in industrial gas-liquid reactions, liquid raw materials usually need to be dissolved, so in this embodiment, a first dissolving tank 1 and a second dissolving tank 3 are provided for dissolving the liquid raw materials. In actual applications, heat exchange jackets or coils can be set on the outside of the first dissolving tank 1 and the second dissolving tank 3 to ensure the dissolution temperature.

[0066] Correspondingly, on the premise of providing the first dissolving tank 1 and the second dissolving tank 3, corresponding first metering pumps 2 and second metering pumps 4 are also provided to achieve quantitative delivery of the liquid raw material.

[0067] In this embodiment, continuous transportation of liquid raw materials can be achieved through alternating transportation of multiple dissolving tanks.

[0068] It should be noted that, in the actual process, the number of dissolving tanks and metering pumps can be determined as needed.

[0069] In a possible implementation, the gas phase feeding system 200 includes a liquid-solid reactor 5 and a gas buffer tank 6:

[0070] The gas outlet of the liquid-solid reactor 5 is connected to the inlet of the gas buffer tank 6, and a mixing plug is provided inside the gas buffer tank 6; the liquid-solid reactor 5 is used to generate gaseous raw materials, the gas buffer tank 6 is used to buffer the generated gaseous raw materials, and the mixing plug is used to achieve gas mixing in the gas buffer tank 6;

[0071] The outlet of the gas buffer tank 6 is connected to the discrete phase side pipeline of the first ejector 7, the discrete phase side pipeline of the third ejector 13, the gas supply port of the first gas-liquid reactor 8, and the gas supply port of the third gas-liquid reactor 14 respectively.

[0072] Specifically, relevant reactions can be carried out in the liquid-solid reactor 5 to generate gaseous raw materials. In practical applications, the liquid-solid reactor 5 can be a single-cantilever conical liquid-solid reactor, and the internal stirring paddle is a single-cantilever stirring paddle, which can rotate while revolving around the axis of the liquid-solid reactor 5, thereby achieving rapid and uniform mixing of materials and rapid removal of reaction heat from the axis to the outer wall of the cone. A heat exchange jacket or coil can be set on the outside of the conical cylinder of the liquid-solid reactor 5; a condenser can be set at the outlet of the liquid-solid reactor 5.

[0073] The inlet of the gas buffer tank 6 can be connected to the gas outlet of the liquid-solid reactor 5, and the outlet of the gas buffer tank 6 is connected to the discrete phase side pipeline of the first ejector 7, the discrete phase side pipeline of the third ejector 13, the gas supply port of the first gas-liquid reactor 8, and the gas supply port of the third gas-liquid reactor 14. The gas buffer tank 6 plays a buffering role on the gas phase raw material from the liquid-solid reactor 5.

[0074] A mixing plug-in may be provided inside the gas buffer tank 6, and when the gaseous raw material is a multi-component gas, uniform mixing of the multi-component gas can be achieved.

[0075] The gas-liquid reaction method based on the gas-liquid reaction system provided by the present application is described below with a method embodiment, and the method comprises:

[0076] S301, the liquid-phase feeding system 100 continuously delivers liquid-phase raw materials to the continuous-phase main pipeline of the first ejector 7, and the gas-phase feeding system 200 synchronously continuously delivers gas-phase raw materials to the discrete-phase side pipeline of the first ejector 7.

[0077] S302 , mixing the liquid raw material provided by the liquid feeding system 100 and the gas raw material provided by the gas feeding system 200 through the first ejector 7 , and conveying the mixed fluid to the first gas-liquid reactor 8 .

[0078] S303, subjecting the liquid raw material and the gas raw material to a gas-liquid reaction through the first gas-liquid reactor 8 to obtain a liquid product, wherein an excess of gas raw material is provided through the gas supply port of the first gas-liquid reactor 8 to ensure that the liquid raw material in the first gas-liquid reactor 8 is fully reacted.

[0079] Specifically, the reaction temperature can be controlled by a heat exchange jacket outside the first gas-liquid reactor 8 .

[0080] S304 , transporting the fluid after the reaction in the first gas-liquid reactor 8 to the first gas-liquid separator 9 , and using the first gas-liquid separator 9 to achieve gas-liquid separation between the liquid phase product of the first gas-liquid reactor 8 and the gas phase raw material that has not reacted completely.

[0081] S305, the liquid phase product separated by the first gas-liquid separator 9 is collected, and the gas phase raw material separated by the first gas-liquid separator 9 is transported to the discrete phase side pipeline of the second ejector 10, and the liquid phase feeding system 100 synchronously transports the liquid phase raw material to the continuous phase main pipeline of the second ejector 10 continuously.

[0082] S306 , mixing the liquid phase raw material provided by the liquid phase feeding system 100 with the gas phase raw material separated by the first gas-liquid separator 9 through the second ejector 10 , and conveying the mixed fluid to the second gas-liquid reactor 11 .

[0083] S307, subjecting the liquid raw material and the gas raw material separated by the first gas-liquid separator 9 to a gas-liquid reaction in the second gas-liquid reactor 11 to obtain a liquid product, wherein an excess of liquid raw material is provided to the second gas-liquid reactor 11 to ensure that the gas raw material in the second gas-liquid reactor 11 is fully reacted.

[0084] Specifically, the reaction temperature can be controlled by a heat exchange jacket outside the second gas-liquid reactor 11 .

[0085] S308, transporting the fluid after the reaction of the second gas-liquid reactor 11 to the second gas-liquid separator 12, and realizing gas-liquid separation between the liquid phase product of the second gas-liquid reactor 11 and the incompletely reacted liquid phase raw materials and the residual gas phase components through the second gas-liquid separator 12.

[0086] S309, the liquid phase product separated by the second gas-liquid separator 12 and the incompletely reacted liquid phase raw material are transported to the continuous phase main pipeline of the third ejector 13, and the gas phase feeding system 200 simultaneously continuously transports the gas phase raw material to the discrete phase side pipeline of the third ejector 13.

[0087] S310, the liquid product of the second gas-liquid reactor 11 and the incompletely reacted liquid raw material are mixed with the gas raw material provided by the gas feeding system 200 through the third ejector 13, and the mixed fluid is transported to the third gas-liquid reactor 14.

[0088] S311, a third gas-liquid reactor 14 is used to carry out a gas-liquid reaction between the incompletely reacted liquid raw material and the gas raw material to obtain a liquid product, wherein an excess of the gas raw material is provided through the gas supply port of the third gas-liquid reactor 14 to ensure that the liquid raw material in the third gas-liquid reactor 14 is fully reacted.

[0089] Specifically, the reaction temperature may be controlled by a heat exchange jacket outside the third gas-liquid reactor 14 .

[0090] S312, transport the fluid after the reaction of the third gas-liquid reactor 14 to the first gas-liquid separator 9, and realize gas-liquid separation between the liquid products of the second gas-liquid reactor 11 and the liquid products of the third gas-liquid reactor 14 and the incompletely reacted gas-phase raw materials through the first gas-liquid separator 9, so as to perform gas-liquid reaction on the incompletely reacted gas-phase raw materials again through the second ejector 10, the second gas-liquid reactor 11, the second gas-liquid separator 12, the third ejector 13 and the third gas-liquid reactor 14.

[0091] Specifically, the liquid phase outlet of the first gas-liquid separator 9 can collect the liquid phase product of the second gas-liquid reactor 11 and the liquid phase product of the third gas-liquid reactor 14 .

[0092] By repeating steps S305 to S311, the gas-phase raw material that has not reacted completely can be subjected to a gas-liquid reaction.

[0093] In a possible implementation, the liquid-phase feeding system 100 continuously delivers the liquid-phase raw material to the continuous phase main line of the first ejector 7, including:

[0094] Dissolving the liquid raw material by the first dissolving tank 1 and the second dissolving tank 3;

[0095] Start the first metering pump 2 to quantitatively transport the liquid phase raw material in the first dissolving tank 1 to the continuous phase main line of the first ejector 7;

[0096] When the liquid raw material in the first dissolving tank 1 is transported, the first metering pump 2 is closed and the second metering pump 4 is started to quantitatively transport the liquid raw material in the second dissolving tank 3 to the continuous phase main line of the first ejector 7, and the liquid raw material is dissolved again through the first dissolving tank 1 so as to start the first metering pump 2 again for continuous transportation of the liquid raw material.

[0097] Specifically, the continuity of the liquid raw material is achieved through the alternating dissolution of the first dissolving tank 1 and the second dissolving tank 3 and the alternating discharge of the first metering pump 2 and the second metering pump 4 .

[0098] It should be noted that the above steps can also be used to realize continuous delivery of the liquid-phase raw material by the liquid-phase feeding system 100 to the continuous phase main pipeline of the second ejector 10 simultaneously.

[0099] In a possible implementation, the gas-phase feeding system 200 synchronously and continuously delivers the gas-phase raw material to the discrete phase side pipeline of the first ejector 7, including:

[0100] Generate gaseous raw materials through liquid-solid reactor 5;

[0101] The gaseous raw material generated by the liquid-solid reactor 5 is transported to the gas buffer tank 6, and the gas in the gas buffer tank 6 is mixed by the mixing plug in the gas buffer tank 6;

[0102] The gaseous raw material in the gas buffer tank 6 is continuously transported to the discrete phase side pipeline of the first ejector 7.

[0103] It should be noted that the above steps can also be used to realize continuous delivery of the gas-phase raw material by the gas-phase feeding system 200 to the discrete phase side pipeline of the third ejector 13 simultaneously.

[0104] The following is an example of the gas-liquid reaction system and the gas-liquid reaction method provided in the embodiment of the present application, in which the lithium fluoride solution and phosphorus pentafluoride gas are mixed to produce a lithium hexafluorophosphate solution. As an electrolyte, lithium hexafluorophosphate is an important core component of the electrolyte of new energy power batteries and is widely used in new energy vehicles, energy storage and other fields:

[0105] Step 1: Continuous delivery of lithium fluoride solution.

[0106] Step 1-1: Inject solid lithium fluoride and AHF solution into the first dissolution tank 1 and the second dissolution tank 3 respectively, and use an external heat exchange jacket or coil AHF solution to control the temperature and dissolve to form a lithium fluoride solution, wherein the mass ratio of lithium fluoride to hydrogen fluoride is 1:5 to 1:25, and the dissolution temperature is -2 to 16°C.

[0107] Step 1-2: Start the first metering pump 2, control the flow rate, and transport the lithium fluoride solution in the first dissolution tank 1 to the continuous phase main line of the first ejector 7.

[0108] Step 1-3: After the lithium fluoride solution in the first dissolution tank 1 is transported, the first metering pump 2 is closed, and the second metering pump 4 is started to transport the lithium fluoride solution in the second dissolution tank 3 to the continuous phase main line of the first ejector 7.

[0109] Step 1-4: while starting the second metering pump 4, close the first metering pump 2, re-inject the solid lithium fluoride and the AHF solution into the first dissolving tank 1, and repeat the feeding operation; the continuous conveying process of the lithium fluoride solution is realized by the alternating feeding, dissolving and discharging process of the dissolving tank; multiple dissolving tanks can be arranged in parallel, and the feeding and dissolving time is less than the continuous conveying time of the material in a single kettle.

[0110] Step 2: Continuous reaction and transportation of phosphorus pentafluoride gas.

[0111] Step 2-1: Start the phosphorus pentachloride continuous automatic feeding device of the liquid-solid reactor 5, continuously inject phosphorus pentachloride solid, and the feeding process is protected by nitrogen; synchronously and continuously inject AHF solution, start the motor, stir, and carry out liquid-solid reaction of phosphorus pentachloride and hydrogen fluoride in the liquid-solid reactor 5 to produce phosphorus pentafluoride gas; use the heat exchange jacket or coil outside the conical cylinder of the liquid-solid reactor 5 to control the reaction temperature. The molar ratio of phosphorus pentachloride to hydrogen fluoride is 1:5.05 to 1:6.65, the reaction temperature of phosphorus pentachloride and hydrogen fluoride is -2 to 16°C, and the rotation and revolution speed of the stirring shaft are 1 to 100 rpm.

[0112] Step 2-2: Open the gas outlet of the liquid-solid reactor 5, recover part of the hydrogen fluoride gas through the condenser, and the mixed gas of phosphorus pentafluoride, hydrogen fluoride, hydrogen chloride, nitrogen, etc. enters the gas buffer tank 6.

[0113] Step 2-3: The mixed gas is mixed evenly by the mixing plug inside the gas buffer tank 6 to ensure the uniformity at the outlet of the gas buffer tank 6. The phosphorus pentafluoride gas content in the mixed gas is 20% to 50%.

[0114] Step 2-4: Start step 2-4 at the same time as starting step 1-2, and transport the mixed gas in the gas buffer tank 6 to the discrete phase side pipeline of the first ejector 7.

[0115] Step 3: Continuous gas-liquid reaction of lithium fluoride solution and phosphorus pentafluoride gas.

[0116] Step 3-1: The first ejector 7 ejects and mixes the lithium fluoride solution from the dissolution tank and the phosphorus pentafluoride gas from the gas buffer tank 6 and enters the first gas-liquid reactor 8.

[0117] Step 3-2: A gas-liquid reaction of fresh lithium fluoride solution and phosphorus pentafluoride is carried out in the first gas-liquid reactor 8, and the reaction temperature is controlled by an external heat exchange jacket; at the same time, phosphorus pentafluoride gas from the gas buffer tank 6 is injected into the gas replenishment port of the first gas-liquid reactor 8 to ensure that the lithium fluoride solution reacts completely. The reaction temperature is -20 to 20°C, the reaction pressure is 0.1 MPa to 2 MPa, and the residence time is 0.5 min to 120 min.

[0118] Step 3-3: The mother liquor and the remaining gas (unreacted phosphorus pentafluoride, hydrogen fluoride, hydrogen chloride, and nitrogen) after the reaction in the first gas-liquid reactor 8 enter the first gas-liquid separator 9, and the gas-liquid separation process is completed in the first gas-liquid separator 9.

[0119] Step 3-4: The remaining gas after separation by the first gas-liquid separator 9 enters the discrete phase side inlet of the second ejector 10; the lithium fluoride solution in the dissolution tank is synchronously transported to the continuous phase main line of the second ejector 10.

[0120] Step 3-5: The second ejector 10 ejects and mixes the lithium fluoride solution from the dissolution tank and the remaining gas separated from the first gas-liquid separator 9 , and the mixture enters the second gas-liquid reactor 11 .

[0121] Step 3-6: The second gas-liquid reactor 11 carries out a gas-liquid reaction between a fresh lithium fluoride solution and the phosphorus pentafluoride gas that has not reacted completely in the first gas-liquid reactor 8, and an excess of lithium fluoride solution is used to ensure that the phosphorus pentafluoride gas reacts completely; the reaction temperature is controlled by an external heat exchange jacket; the reaction temperature is -20 to 20°C; the reaction pressure is 0.1 MPa to 2 MPa; and the residence time is 0.5 min to 120 min.

[0122] Step 3-7: The mother liquor and the remaining gas (hydrogen fluoride, hydrogen chloride, nitrogen) after the reaction in the second gas-liquid reactor 11 enter the second gas-liquid separator 12, and the gas-liquid separation process is completed in the second gas-liquid separator 12.

[0123] Step 3-8: The mother liquor (product lithium hexafluorophosphate and remaining lithium fluoride solution) separated by the second gas-liquid separator 12 enters the continuous phase inlet of the third ejector 13 from the liquid phase outlet of the second gas-liquid separator 12; the fresh gas from the gas buffer tank 6 simultaneously enters the discrete phase side pipeline of the third ejector 13.

[0124] Step 3-9: The third ejector 13 is used to eject and mix the product lithium hexafluorophosphate from the second gas-liquid separator 12 , the remaining lithium fluoride solution and the fresh gas from the gas buffer tank 6 into the third gas-liquid reactor 14 .

[0125] Step 3-10: A gas-liquid reaction is carried out in the third gas-liquid reactor 14 between the lithium fluoride solution that has not been completely reacted in the second gas-liquid reactor 11 and the fresh phosphorus pentafluoride gas. At the same time, the fresh gas from the gas buffer tank 6 enters the gas replenishment port of the third gas-liquid reactor 14. The phosphorus pentafluoride is in excess to ensure that the lithium fluoride solution reacts completely. The reaction temperature is -20 to 20°C, the reaction pressure is 0.1 MPa to 2 MPa, and the residence time is 0.5 min to 120 min.

[0126] Step 3-11: the mother liquid and the remaining gas after the reaction in the third gas-liquid reactor 14 enter the first gas-liquid separator 9 again; repeat steps 3-4 to 3-10 to achieve continuous gas-liquid reaction.

[0127] It can be seen that the present application provides a gas-liquid reaction system and a gas-liquid reaction method, the system includes a liquid phase feeding system, a gas phase feeding system, a first ejector, a first gas-liquid reactor, a first gas-liquid separator, a second ejector, a second gas-liquid reactor, a second gas-liquid separator, a third ejector, and a third gas-liquid reactor: the liquid phase feeding system is connected to the continuous phase main line of the first ejector and the continuous phase main line of the second ejector respectively; the gas phase feeding system is connected to the discrete phase side pipeline of the first ejector, the discrete phase side pipeline of the third ejector, the gas supply port of the first gas-liquid reactor, and the gas supply port of the third gas-liquid reactor respectively; the outlet of the first ejector is connected to the inlet of the first gas-liquid reactor, and the first gas-liquid reactor The outlet of the first gas-liquid separator is connected to the inlet of the first gas-liquid separator; the first ejector is used to mix the liquid raw material provided by the liquid feeding system with the gas raw material provided by the gas feeding system, and the first gas-liquid reactor is used for the liquid raw material and the gas raw material to carry out a gas-liquid reaction to obtain a liquid product, wherein the gas replenishing port of the first gas-liquid reactor is used to provide an excess of gas raw material to ensure that the liquid raw material in the first gas-liquid reactor is fully reacted, and the first gas-liquid separator is used to achieve gas-liquid separation between the liquid product of the first gas-liquid reactor and the gas raw material that has not reacted completely; the gas phase outlet of the first gas-liquid separator is connected to the discrete phase side pipeline of the second ejector, the outlet of the second ejector is connected to the inlet of the second gas-liquid reactor, and the second gas-liquid reactor The outlet of the second gas-liquid separator is connected to the inlet of the second gas-liquid separator; the second ejector is used to mix the liquid raw material provided by the liquid feeding system with the gas raw material separated by the first gas-liquid separator, and the second gas-liquid reactor is used to carry out gas-liquid reaction between the liquid raw material and the gas raw material separated by the first gas-liquid separator to obtain a liquid product, wherein the excess liquid raw material in the second gas-liquid reactor is used to ensure that the gas raw material in the second gas-liquid reactor is fully reacted, and the second gas-liquid separator is used to separate the liquid product of the second gas-liquid reactor and the liquid raw material that has not reacted completely from the residual gas components; the liquid phase outlet of the second gas-liquid separator is connected to the continuous phase main pipeline of the third ejector, and the outlet of the third ejector is connected to the inlet of the third gas-liquid reactor. The outlet of the third gas-liquid reactor is connected to the inlet of the first gas-liquid separator; the third ejector is used to mix the liquid product of the second gas-liquid reactor and the liquid raw material that has not reacted completely with the gas raw material provided by the gas feeding system; the third gas-liquid reactor is used to carry out gas-liquid reaction between the liquid raw material that has not reacted completely in the second gas-liquid reactor and the gas raw material provided by the gas feeding system to obtain a liquid product, wherein the gas replenishing port of the third gas-liquid reactor is used to provide excess gas raw material to ensure that the liquid raw material in the third gas-liquid reactor is fully reacted, and the first gas-liquid separator is also used to achieve gas-liquid separation between the liquid product of the second gas-liquid reactor and the liquid product of the third gas-liquid reactor and the gas raw material that has not reacted completely.For the above-mentioned gas-liquid reaction system, a continuous reaction of liquid-phase raw materials and gas-phase raw materials is achieved through multiple groups of gas-liquid reactors and gas-liquid separators, wherein the first gas-liquid reactor is used to complete the reaction of the liquid-phase raw materials, the first gas-liquid separator is used to recover the excess gas-phase raw materials and collect the liquid-phase products produced by the first gas-liquid reactor, the second gas-liquid reactor is used to complete the reaction of the excess gas-phase raw materials, the second gas-liquid separator is used to recover the excess liquid-phase raw materials, the third gas-liquid reactor is used to complete the reaction of the excess liquid-phase raw materials, and the first gas-liquid separator is used to collect the liquid-phase products produced by the second gas-liquid reactor and the third gas-liquid reactor. That is, in the continuous reaction process, on the one hand, the gas-phase raw materials and the liquid-phase raw materials are fully reacted, and the product quality is guaranteed by avoiding the mixing of the liquid-phase raw materials and the liquid-phase products. On the other hand, the maximum utilization of the liquid-phase raw materials and the gas-phase raw materials is achieved, thereby saving production costs.

[0128] In the description of this specification, the description with reference to the terms "some possible embodiments", "some embodiments", "examples", "specific examples", or "some examples" means that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present application, and the above terms do not necessarily represent the same embodiment or example. Moreover, the described specific features, structures, materials or characteristics may be combined in any one or more embodiments or examples in a suitable manner. In addition, those skilled in the art may combine and combine the different embodiments or examples described in this specification and the features of the different embodiments or examples, unless they are contradictory.

[0129] Although the spirit and principle of the present application have been described above with reference to several specific embodiments, it should be understood that the present application is not limited to the disclosed specific embodiments, and the division of various aspects does not mean that the features in these aspects cannot be combined. The present application is intended to cover various modifications and equivalent arrangements included in the spirit and scope of the attached claims.

Claims

1. A gas-liquid reaction system, characterized in that: The system comprises a liquid phase feeding system (100), a gas phase feeding system (200), a first ejector (7), a first gas-liquid reactor (8), a first gas-liquid separator (9), a second ejector (10), a second gas-liquid reactor (11), a second gas-liquid separator (12), a third ejector (13), and a third gas-liquid reactor (14): The liquid phase feeding system (100) is connected to the continuous phase main line of the first ejector (7) and the continuous phase main line of the second ejector (10), respectively; The gas phase feeding system (200) is respectively connected to the discrete phase side pipeline of the first ejector (7), the discrete phase side pipeline of the third ejector (13), the gas supply port of the first gas-liquid reactor (8), and the gas supply port of the third gas-liquid reactor (14); The outlet of the first ejector (7) is connected to the inlet of the first gas-liquid reactor (8), and the outlet of the first gas-liquid reactor (8) is connected to the inlet of the first gas-liquid separator (9); the first ejector (7) is used to mix the liquid raw material provided by the liquid feeding system (100) with the gas raw material provided by the gas feeding system (200); the first gas-liquid reactor (8) is used to react the liquid raw material with the gas raw material to obtain a liquid product; wherein the gas replenishing port of the first gas-liquid reactor (8) is used to provide an excess of gas raw material to ensure that the liquid raw material in the first gas-liquid reactor (8) is fully reacted; and the first gas-liquid separator (9) is used to separate the liquid product of the first gas-liquid reactor (8) from the gas raw material that has not reacted completely; The gas phase outlet of the first gas-liquid separator (9) is connected to the discrete phase side pipeline of the second ejector (10), the outlet of the second ejector (10) is connected to the inlet of the second gas-liquid reactor (11), and the outlet of the second gas-liquid reactor (11) is connected to the inlet of the second gas-liquid separator (12); the second ejector (10) is used to mix the liquid phase raw material provided by the liquid phase feeding system (100) with the gas phase raw material separated by the first gas-liquid separator (9), and the second gas-liquid reactor (11) is used to react the liquid phase raw material with the gas phase raw material separated by the first gas-liquid separator (9) to obtain a liquid phase product, wherein the excess liquid phase raw material in the second gas-liquid reactor (11) is used to ensure that the gas phase raw material in the second gas-liquid reactor (11) is fully reacted, and the second gas-liquid separator (12) is used to separate the liquid phase product of the second gas-liquid reactor (11) and the liquid phase raw material that has not reacted completely from the residual gas phase components; The liquid phase outlet of the second gas-liquid separator (12) is connected to the continuous phase main pipeline of the third ejector (13), the outlet of the third ejector (13) is connected to the inlet of the third gas-liquid reactor (14), and the outlet of the third gas-liquid reactor (14) is connected to the inlet of the first gas-liquid separator (9); the third ejector (13) is used to mix the liquid phase product and the incompletely reacted liquid phase raw material of the second gas-liquid reactor (11) with the gas phase raw material provided by the gas phase feeding system (200), and the third gas-liquid reactor (14) is used to mix the liquid phase product and the incompletely reacted liquid phase raw material of the second gas-liquid reactor (11) with the gas phase raw material provided by the gas phase feeding system (200). ) is used for gas-liquid reaction between the liquid-phase raw material that has not been completely reacted in the second gas-liquid reactor (11) and the gas-phase raw material provided by the gas-phase feeding system (200) to obtain a liquid-phase product, wherein the gas replenishing port of the third gas-liquid reactor (14) is used to provide excess gas-phase raw material to ensure that the liquid-phase raw material in the third gas-liquid reactor (14) is fully reacted, and the first gas-liquid separator (9) is also used to achieve gas-liquid separation between the liquid-phase product of the second gas-liquid reactor (11) and the liquid-phase product of the third gas-liquid reactor (14) and the gas-phase raw material that has not been completely reacted.

2. The gas-liquid reaction system according to claim 1, characterized in that: The first gas-liquid reactor (8) comprises a plurality of reaction pipelines and a plurality of series structures (83), wherein the plurality of reaction pipelines are arranged in parallel, and the series structure (83) is used to connect two adjacent reaction pipelines.

3. The gas-liquid reaction system according to claim 2, characterized in that: The first gas-liquid reactor (8) further comprises a plurality of static mixing inserts (82), wherein the plurality of static mixing inserts (82) are distributed in the plurality of reaction pipelines, and the static mixing inserts (82) have a cutting surface.

4. The gas-liquid reaction system according to claim 3, characterized in that: The first gas-liquid reactor (8) further comprises a gas supply pipeline (81), and an outlet of the gas supply pipeline (81) is arranged inside any reaction pipeline among the multiple reaction pipelines.

5. The gas-liquid reaction system according to claim 4, characterized in that: A heat exchange jacket is arranged outside the first gas-liquid reactor (8).

6. The gas-liquid reaction system according to claim 1, characterized in that: The liquid phase feeding system (100) comprises a first dissolving tank (1), a first metering pump (2), a second dissolving tank (3), and a second metering pump (4): The outlet of the first dissolving tank (1) is connected to the inlet of the first metering pump (2), and the outlet of the first metering pump (2) is respectively connected to the continuous phase main line of the first ejector (7) and the continuous phase main line of the second ejector (10); the first dissolving tank (1) is used for dissolving the liquid raw material, and the first metering pump (2) is used for quantitatively conveying the liquid raw material; The outlet of the second dissolving tank (3) is connected to the inlet of the second metering pump (4), and the outlet of the second metering pump (4) is respectively connected to the continuous phase main line of the first ejector (7) and the continuous phase main line of the second ejector (10); the second dissolving tank (3) is used to dissolve the liquid raw material, and the second metering pump (4) is used to quantitatively transport the liquid raw material.

7. The gas-liquid reaction system according to claim 1, characterized in that: The gas phase feeding system (200) comprises a liquid-solid reactor (5) and a gas buffer tank (6): The gas outlet of the liquid-solid reactor (5) is connected to the inlet of the gas buffer tank (6), and a mixing plug is provided inside the gas buffer tank (6); the liquid-solid reactor (5) is used to generate gaseous raw materials, the gas buffer tank (6) is used to buffer the generated gaseous raw materials, and the mixing plug is used to achieve gas mixing in the gas buffer tank (6); The outlet of the gas buffer tank (6) is respectively connected to the discrete phase side pipeline of the first ejector (7), the discrete phase side pipeline of the third ejector (13), the gas supply port of the first gas-liquid reactor (8), and the gas supply port of the third gas-liquid reactor (14).

8. A gas-liquid reaction method based on the gas-liquid reaction system according to any one of claims 1 to 7, characterized in that: The method comprises: The liquid phase feeding system (100) continuously delivers liquid phase raw materials to the continuous phase main pipeline of the first ejector (7), and the gas phase feeding system (200) synchronously continuously delivers gas phase raw materials to the discrete phase side pipeline of the first ejector (7); The liquid raw material provided by the liquid-phase feeding system (100) is mixed with the gas-phase raw material provided by the gas-phase feeding system (200) through the first ejector (7), and the mixed fluid is transported to the first gas-liquid reactor (8); The first gas-liquid reactor (8) is used to carry out a gas-liquid reaction between a liquid-phase raw material and a gas-phase raw material to obtain a liquid-phase product, wherein an excess of the gas-phase raw material is provided through the gas supply port of the first gas-liquid reactor (8) to ensure that the liquid-phase raw material in the first gas-liquid reactor (8) is fully reacted; The fluid after the reaction in the first gas-liquid reactor (8) is transported to the first gas-liquid separator (9), and the first gas-liquid separator (9) is used to achieve gas-liquid separation between the liquid phase product of the first gas-liquid reactor (8) and the gas phase raw material that has not reacted completely; The liquid phase product separated by the first gas-liquid separator (9) is collected, and the gas phase raw material separated by the first gas-liquid separator (9) is transported to the discrete phase side pipeline of the second ejector (10), and the liquid phase feeding system (100) simultaneously continuously transports the liquid phase raw material to the continuous phase main pipeline of the second ejector (10); The liquid phase raw material provided by the liquid phase feeding system (100) is mixed with the gas phase raw material separated by the first gas-liquid separator (9) through the second ejector (10), and the mixed fluid is transported to the second gas-liquid reactor (11); The liquid raw material and the gas raw material separated by the first gas-liquid separator (9) are subjected to a gas-liquid reaction by the second gas-liquid reactor (11) to obtain a liquid product, wherein an excess of liquid raw material is provided to the second gas-liquid reactor (11) to ensure that the gas raw material in the second gas-liquid reactor (11) is fully reacted; The fluid after the reaction in the second gas-liquid reactor (11) is transported to the second gas-liquid separator (12), and the second gas-liquid separator (12) is used to separate the liquid phase product of the second gas-liquid reactor (11) from the liquid phase raw material that has not reacted completely and the residual gas phase components; The liquid phase product separated by the second gas-liquid separator (12) and the incompletely reacted liquid phase raw material are transported to the continuous phase main pipeline of the third ejector (13), and the gas phase feeding system (200) simultaneously continuously transports the gas phase raw material to the discrete phase side pipeline of the third ejector (13); The liquid phase product and the incompletely reacted liquid phase raw material of the second gas-liquid reactor (11) are mixed with the gas phase raw material provided by the gas phase feeding system (200) through the third ejector (13), and the mixed fluid is transported to the third gas-liquid reactor (14); The third gas-liquid reactor (14) is used to carry out a gas-liquid reaction between the incompletely reacted liquid raw material and the gas raw material to obtain a liquid product, wherein an excess of the gas raw material is provided through the gas supply port of the third gas-liquid reactor (14) to ensure that the liquid raw material in the third gas-liquid reactor (14) is fully reacted; The fluid after the reaction of the third gas-liquid reactor (14) is transported to the first gas-liquid separator (9), and the liquid phase product of the second gas-liquid reactor (11) and the liquid phase product of the third gas-liquid reactor (14) are separated from the gas phase raw material that has not reacted completely by the first gas-liquid separator (9), so that the gas phase raw material that has not reacted completely can be subjected to gas-liquid reaction again by the second ejector (10), the second gas-liquid reactor (11), the second gas-liquid separator (12), the third ejector (13) and the third gas-liquid reactor (14).

9. The gas-liquid reaction method according to claim 8, characterized in that: The liquid phase feeding system (100) continuously delivers liquid phase raw materials to the continuous phase main pipeline of the first ejector (7), comprising: Dissolving the liquid raw material by means of a first dissolving tank (1) and a second dissolving tank (3); Starting the first metering pump (2) to quantitatively transport the liquid phase raw material in the first dissolving tank (1) to the continuous phase main line of the first ejector (7); After the liquid raw material in the first dissolving tank (1) is transported, the first metering pump (2) is closed and the second metering pump (4) is started to quantitatively transport the liquid raw material in the second dissolving tank (3) to the continuous phase main line of the first ejector (7), and the liquid raw material is dissolved again through the first dissolving tank (1) so that the first metering pump (2) can be started again to continuously transport the liquid raw material.

10. The gas-liquid reaction method according to claim 8, characterized in that: The gas phase feeding system (200) synchronously and continuously delivers gas phase raw materials to the discrete phase side pipeline of the first ejector (7), comprising: Generating a gaseous raw material through a liquid-solid reactor (5); The gaseous raw material generated by the liquid-solid reactor (5) is transported to a gas buffer tank (6), and the gas in the gas buffer tank (6) is mixed by a mixing plug in the gas buffer tank (6); The gaseous raw material in the gas buffer tank (6) is continuously transported to the discrete phase side pipeline of the first ejector (7).

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