CN218166971U - Gas-liquid mixing reaction device and reaction system with same - Google Patents

Abstract

The utility model provides a gas-liquid mixture reaction unit and have its reaction system, gas-liquid mixture reaction unit includes: the shell is provided with a primary mixing section, a primary reaction section, a secondary mixing section and a secondary reaction section which are communicated in sequence; the first gas-liquid distributor is arranged in the primary mixing section, and the aperture ratio of the first gas-liquid distributor is 10-50%; the primary jacket is arranged on the periphery of the shell and used for heating a gas-liquid mixture in the primary reaction section; the second gas-liquid distributor is arranged in the secondary mixing section and is provided with through holes; and the secondary jacket is arranged on the periphery of the shell and positioned on the outer side of the secondary reaction section, and is used for heating the gas-liquid mixture in the secondary reaction section. Through the technical scheme that this application provided, can solve the gas-liquid mixture among the prior art back mixing degree height and the bubble and produce the problem of gathering the phenomenon easily.

Description

Gas-liquid mixing reaction device and reaction system with same

Technical Field

The utility model relates to a gas-liquid mixture reaction technical field particularly, relates to a gas-liquid mixture reaction unit and have its reaction system.

Background

The gas-liquid reaction is a common reaction form in the chemical production process, most of the current gas-liquid mixing reaction devices are bubble tower reactors, the bubble tower reactors are provided with distributors at the bottoms of the towers, the distributors are usually designed into pore plate structures, and gas flows upwards from the bottoms of the towers through liquid layers in a bubble form after passing through the distributors and is mixed with the liquid.

However, in the prior art, because the reaction volume inside the bubble column reactor is large, the gas-liquid mixture is very likely to generate a back-mixing phenomenon when flowing inside the reactor, which reduces the controllability of the reaction process and further reduces the selectivity and yield of the reaction product, and the bubble is very likely to generate a coalescence phenomenon in the upward flowing process, which reduces the contact area of the gas and the liquid, thereby reducing the gas-liquid mass transfer efficiency and further deteriorating the reaction effect of the gas-liquid mixture.

SUMMERY OF THE UTILITY MODEL

The utility model provides a gas-liquid mixture reaction unit and have its reaction system to the gas-liquid mixture backmixing degree that solves among the prior art is high and the bubble produces the problem of gathering the phenomenon easily.

According to an aspect of the utility model, a gas-liquid mixture reaction unit is provided, and gas-liquid mixture reaction unit includes: the shell is provided with a primary mixing section, a primary reaction section, a secondary mixing section and a secondary reaction section which are sequentially communicated, and is also provided with a gas inlet, a liquid inlet and an outlet, wherein the gas inlet and the liquid inlet are both communicated with the first section of the primary mixing section, and the outlet is communicated with the tail end of the secondary reaction section; the first gas-liquid distributor is arranged in the primary mixing section, through holes are formed in the first gas-liquid distributor, and the opening rate of the first gas-liquid distributor is 10% -50%; the primary jacket is arranged on the periphery of the shell and positioned on the outer side of the primary reaction section, and is used for heating a gas-liquid mixture in the primary reaction section; the second gas-liquid distributor is arranged in the secondary mixing section and is provided with through holes; and the secondary jacket is arranged at the periphery of the shell and positioned at the outer side of the secondary reaction section, and is used for heating the gas-liquid mixture of the secondary reaction section.

Furthermore, first gas-liquid distributor has mixed import, mixing chamber and mixed export, mixes the import and communicates with gas feed and liquid inlet respectively, mixes import and mixed export and is located the both ends of first gas-liquid distributor respectively, has a plurality of liquid holes on the first gas-liquid distributor.

Further, the aperture ratio of the first gas-liquid distributor is 30% to 40%.

Further, the opening rate of the second gas-liquid distributor is 30% to 70%.

Further, the ratio of the height to the aperture diameter of the first gas-liquid distributor is in the range of 1 to 10.

Furthermore, a plurality of temperature measuring ports are arranged on the shell, the temperature measuring ports are communicated with the inside of the shell, at least one temperature measuring port is arranged close to the first section of the primary reaction section, at least one temperature measuring port is arranged close to the secondary mixing section, and at least one temperature measuring port is arranged close to the tail end of the secondary reaction section.

Further, detachably be provided with the end plate on the casing, the end plate is close to the primary mixing section and sets up, and first gas-liquid distributor sets up on the end plate.

According to the utility model discloses an on the other hand provides a reaction system, and reaction system includes: the gas-liquid mixing reaction device is the gas-liquid mixing reaction device; the material storage device is communicated with the outlet of the gas-liquid mixing reaction device; and the tail gas treatment component is communicated with an outlet of the gas-liquid mixing reaction device.

Further, the reaction system further comprises: the temperature detection piece is arranged at a temperature measuring port of the gas-liquid mixing reaction device; the temperature adjusting component is connected with the primary jacket and the secondary jacket and can adjust the temperature of a heat exchange medium in the jacket of the gas-liquid mixing reaction device; and the control part is respectively electrically connected with the temperature detection part and the temperature adjusting component and controls the temperature adjusting component to adjust the temperature of the heat exchange medium according to the data detected by the temperature detection part.

Further, the exhaust treatment assembly includes: the gas-liquid separator is provided with a material inlet, a tail gas outlet and a material outlet, the material inlet is communicated with the outlet of the gas-liquid mixing reaction device, and the material outlet is communicated with the inlet of the material storage device; the tail gas condensing device is provided with a condensing inlet and a condensing outlet, and the condensing inlet is communicated with the tail gas outlet; and the tail gas absorption device is communicated with the condensation outlet.

Use the technical scheme of the utility model, gas and liquid mix after gas feed and liquid feed entering primary mixing section respectively, because be provided with first gas-liquid distributor in the primary mixing section, first gas-liquid distributor can evenly cut gas into a plurality of small bubbles, first gas-liquid distributor also can be split into the droplet with liquid simultaneously, can make the droplet fully contact with small bubble like this, and then make liquid and gas can mix evenly in primary mixing section, thereby can reinforce gas-liquid mass transfer effect, gas can drive liquid flow to primary reaction section in, and can make the gas-liquid mixture get into the abundant reaction behind the primary reaction section. In the upward flowing process of the gas-liquid mixture, small bubbles can be gradually enlarged and even generate coalescence phenomenon due to the influence of conditions such as pressure, reaction temperature and the like, and the gas-liquid mixing effect is influenced. In this application, first gas-liquid distributor and second gas-liquid distributor separate the casing for primary reaction section and secondary reaction section, separate the inside reaction zone of casing for a plurality of reaction sections like this, can reduce the volume of every reaction section, thereby can make gas-liquid mixture be similar to the plug flow when flowing in the casing, greatly reduced the back mixing degree of gas-liquid mixture in the casing, can avoid the small bubble to produce simultaneously and gather and the phenomenon, the controllability of reaction process has been improved, thereby can further improve the selectivity and the yield of reaction product.

Drawings

The accompanying drawings, which form a part of the present application, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention and not to limit the invention. In the drawings:

FIG. 1 shows a schematic structural diagram of a gas-liquid mixing reactor provided by the present invention;

fig. 2 shows a schematic structural diagram of a reaction system provided by the present invention.

Wherein the figures include the following reference numerals:

10. a housing; 11. a primary mixing section; 12. a primary reaction section; 13. a secondary mixing section; 14. a secondary reaction section; 15. a gas inlet; 16. a liquid inlet; 17. an outlet; 18. a temperature measuring port; 19. an end plate;

20. a first gas-liquid distributor;

30. a primary jacket;

40. a second gas-liquid distributor;

50. secondary jacket;

61. a material storage device; 62. a gas-phase steel cylinder; 63. a liquid phase raw material storage tank; 64. a material-beating pump; 65. a liquid mass flow meter; 66. a gas mass flow meter;

70. a tail gas treatment component; 71. a gas-liquid separator; 72. a tail gas condensing device; 73. a tail gas absorption device;

81. a temperature detection member; 82. a temperature regulating component; 821. a first temperature control device; 822. a second temperature control device; 83. and a control member.

Detailed Description

The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. The following description of at least one exemplary embodiment is merely illustrative in nature and is in no way intended to limit the invention, its application, or uses. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.

As shown in fig. 1, an embodiment of the present invention provides a gas-liquid mixing reaction apparatus, which includes a housing 10, a first gas-liquid distributor 20, a primary jacket 30, a second gas-liquid distributor 40, and a secondary jacket 50. The shell 10 is provided with a primary mixing section 11, a primary reaction section 12, a secondary mixing section 13 and a secondary reaction section 14 which are sequentially communicated, the shell 10 is also provided with a gas inlet 15, a liquid inlet 16 and an outlet 17, the gas inlet 15 and the liquid inlet 16 are both communicated with the first section of the primary mixing section 11, and the outlet 17 is communicated with the tail end of the secondary reaction section 14. The first gas-liquid distributor 20 is arranged in the primary mixing section 11, through holes are arranged on the first gas-liquid distributor 20, and the aperture ratio of the first gas-liquid distributor 20 is 10% to 50%. The primary jacket 30 is disposed at the periphery of the shell 10 and located outside the primary reaction section 12, and the primary jacket 30 is used for heating the gas-liquid mixture in the primary reaction section 12. The second gas-liquid distributor 40 is arranged in the secondary mixing section 13, and through holes are formed in the second gas-liquid distributor 40. The secondary jacket 50 is arranged on the periphery of the shell 10 and is located outside the secondary reaction section 14, and the secondary jacket 50 is used for heating the gas-liquid mixture in the secondary reaction section 14.

Use the technical scheme of this application, gaseous and liquid mix after getting into primary mixing section 11 through gas inlet 15 and liquid inlet 16 respectively, because be provided with first gas-liquid distributor 20 in the primary mixing section 11, first gas-liquid distributor 20 can be with gaseous even cutting for a plurality of small bubbles, first gas-liquid distributor 20 also can be cut apart into the droplet with liquid simultaneously, can make the droplet fully contact with small bubble like this, and then make liquid and gaseous even in mixing section 11, thereby can strengthen the gas-liquid mass transfer effect, gaseous can drive liquid flow to primary mixing section 11 in, and can make the gas-liquid mixture get into the fully reaction behind the primary reaction section 12. In the upward flowing process of the gas-liquid mixture, small bubbles can be gradually enlarged and even generate coalescence phenomenon due to the influence of conditions such as pressure, reaction temperature and the like, and the gas-liquid mixing effect is influenced. In the present application, the first gas-liquid distributor 20 and the second gas-liquid distributor 40 separate the casing 10 into the first reaction section 12 and the second reaction section 14, so as to separate the reaction area inside the casing 10 into a plurality of reaction sections, and can reduce the volume of each reaction section, thereby enabling the gas-liquid mixture to be similar to plug flow when flowing in the casing 10, greatly reducing the back mixing degree of the gas-liquid mixture in the casing 10, and simultaneously avoiding the coalescence phenomenon of small bubbles, improving the controllability of the reaction process, and further improving the selectivity and yield of the reaction product. Preferably, for further avoiding the small bubbles to produce the coalescence phenomenon and further reducing the back mixing degree of the gas-liquid mixture, can calculate through hydrodynamics simulation and pass through behind gas and liquid through first gas-liquid distributor 20, the height that the bubbles produced coalescence under different operating modes, and then can begin to coalesce the position at the bubble and set up second gas-liquid distributor 40, and set up second distribution baffle in secondary mixing section 13, ensure that gas forms with the small bubbles all the time and mixes with liquid contact, promote the system to continuously react stably, strengthen the mass transfer effect of gas and liquid in secondary reaction section 14, make the reaction more abundant.

Further, first gas-liquid distributor 20 has mixed import, mixing chamber and mixed export, mixes the import and communicates with gas inlet 15 and liquid inlet 16 respectively, mixes import and mixed export and is located the both ends of first gas-liquid distributor 20 respectively, has a plurality of liquid holes on the first gas-liquid distributor 20. Wherein, in this application, first gas-liquid distributor 20 is the tubular structure, is provided with the opening on the first gas-liquid distributor 20, and the lateral wall and the bottom of first gas-liquid distributor 20 all are provided with a plurality of liquid holes, and the opening on the first gas-liquid distributor 20 is mixed the import, and the liquid hole that goes out on lateral wall and the bottom is mixed the export to, the volume size of the hybrid chamber of first gas-liquid distributor 20 can be designed according to gas-liquid feeding flow size and dwell time. By adopting the structure, the structure is simple, and the gas and the liquid can be immediately and respectively divided into small bubbles and liquid drops through the first gas-liquid distributor 20 after being mixed, so that the reaction of the gas and the liquid is facilitated. In the prior art, the gas-liquid mixing and gas-liquid reaction are respectively and independently provided with two structures, and raw materials subjected to gas-liquid mixing are sent into the gas-liquid reaction part through a pipeline to react, so that the gas-liquid mixing effect is weakened. In the application, in the gas-liquid mixing reaction device, gas and liquid can be directly reacted after being mixed, so that the gas-liquid mixing effect during reaction can be ensured, the reaction speed is improved, the reaction time is shortened, the unit operation times can be reduced, the equipment investment is reduced, and the yield of reaction products is improved. Alternatively, the first gas-liquid distributor 20 may be a static mixer, and the specific form of the static mixer may be any one of SK type, SV type, SH type, or SX type.

The opening rate of the first gas-liquid distributor 20 is set to be between 10% and 50%, and when the opening rate of the first gas-liquid distributor 20 is less than 10%, the gas and the liquid are easy to block when passing through the first gas-liquid distributor 20, so that the normal flow of the gas and the liquid is influenced; when the aperture ratio of the first gas-liquid distributor 20 is greater than 50%, the bubbles separated by the first gas-liquid distributor 20 are too many, so that the possibility of the coalescence of the bubbles is improved, and the mixing time of the gas and the liquid in the primary mixing section 11 is reduced, thereby causing poor mixing effect of the gas and the liquid; consequently, set up the percent opening of first gas-liquid distributor 20 between 10% to 50%, can enough guarantee like this that gas and liquid flow's smoothness nature, and then guarantee that gas-liquid mixing device can normally work, can guarantee the mixing effect of gas and liquid in primary mixing section 11 simultaneously, further strengthen the mass transfer effect of gas and liquid.

The primary jacket 30 and the secondary jacket 50 can respectively heat the primary reaction section 12 and the secondary reaction section 14, so that the gas-liquid mixing reaction device can meet the requirements of gas and liquid during reaction, and is simple in structure and convenient to operate. Moreover, because the gas and the liquid usually emit heat during the reaction, when the primary reaction section 12 and the secondary reaction section 14 are heated separately, the temperature of the heat exchange medium in the primary jacket 30 can be higher than the temperature of the heat exchange medium in the secondary jacket 50, so that the temperature consistency in the primary reaction section 12 and the secondary reaction section 14 can be ensured, the consistency of the product after the gas and the liquid react can be ensured, and the yield of the reaction product can be further improved. In the present application, 316L stainless steel, titanium steel, etc. can be selected as the material of the housing 10, and tetrafluoro spray coating, etc. can be adopted as the material with strong corrosion.

In the present embodiment, the aperture ratio of the first gas-liquid distributor 20 is 30% to 40%. So can further guarantee the smooth and easy nature that gas and liquid flow, and then can guarantee that gas-liquid mixing device normally works, can further guarantee the mixing effect of gas and liquid in primary mixing section 11 simultaneously, further strengthen the mass transfer effect of gas and liquid.

Wherein the opening rate of the second gas-liquid distributor 40 is 30% to 70%. When the opening rate of the second gas-liquid distributor 40 is less than 30%, the gas and the liquid are easy to block when passing through the second gas-liquid distributor 40, and the normal flow of the gas and the liquid is influenced; when the opening ratio of the second gas-liquid distributor 40 is greater than 70%, the bubbles separated by the second gas-liquid distributor 40 are excessive, the possibility of the bubble coalescence is improved, and the mixing time of the gas and the liquid in the secondary mixing section 13 is reduced, so that the mixing effect of the gas and the liquid is poor. Therefore, through computational fluid dynamics simulation calculation, the opening rate of the second gas-liquid distributor 40 is set to be 30% to 70%, so that the smoothness of the flowing of the gas and the liquid can be ensured, the mixing effect of the gas and the liquid in the secondary mixing section 13 can be ensured, and the mass transfer effect of the gas and the liquid is further enhanced. Preferably, the opening ratio of the second gas-liquid distributor 40 is set to 40% to 60%.

Further, the ratio of the height to the aperture diameter of the first gas-liquid distributor 20 is in the range of 1 to 10. In this application, first gas-liquid distributor 20 is tubular structure, and the ratio of the height of first gas-liquid distributor 20 to the internal aperture is in the range of 1 to 10, so set up, can make gas and liquid fully mix in tubular structure to can reduce the amplification effect that causes because liquid maldistribution. The residence time of the reaction raw materials in the cavity is kept in the range of 0.1 to 3s so as to meet the requirement of optimal mixing effect under different feeding amounts. In the present application, the material of the first gas-liquid distributor 20 may be 316L stainless steel, titanium steel, hastelloy, or the like.

Specifically, a plurality of temperature measuring ports 18 are arranged on the shell 10, the temperature measuring ports 18 are all communicated with the inside of the shell 10, at least one temperature measuring port 18 is arranged close to the first section of the primary reaction section 12, at least one temperature measuring port 18 is arranged close to the secondary mixing section 13, and at least one temperature measuring port 18 is arranged close to the tail end of the secondary reaction section 14. Because in the chemical reaction process, the reaction temperature has great influence on the chemical reaction, so the arrangement is adopted, the staff can record the temperature change in real time through the temperature measuring port 18, and the accurate temperature detection is provided for the gas-liquid mixing reaction device, thereby the yield of the reaction product can be further improved, and other byproducts are avoided being produced in the reaction process.

Specifically, the housing 10 is detachably provided with an end plate 19, the end plate 19 is disposed near the primary mixing section 11, and the first gas-liquid distributors 20 are disposed on the end plate 19. In this application, end plate 19 is lower flange to be provided with the flange on casing 10, the lower flange can be dismantled with last flange and be connected, so set up, simple structure is convenient for dismantle first gas-liquid distributor 20, and then the washing to gas-liquid distributor in the later stage use of being convenient for is maintained, also can change first gas-liquid distributor 20 according to the filler volume simultaneously. Alternatively, the end plate 19 may be directly welded to the housing 10, or a quick-opening connection may be used between the end plate 19 and the housing 10.

As shown in fig. 2, another embodiment of the present application provides a reaction system, which includes a gas-liquid mixing reaction device, a storage device 61, and a tail gas treatment assembly 70. Gas-liquid mixture reaction unit is the above-mentioned gas-liquid mixture reaction unit who provides, and storage device 61 communicates with gas-liquid mixture reaction unit's export 17, and storage device 61 can collect the product that produces after the reaction. Tail gas treatment component 70 and gas-liquid mixture reaction unit's export 17 intercommunication, tail gas treatment component 70 can collect the tail gas that produces after the reaction, avoids tail gas to staff's health and surrounding environment to produce the injury to the staff can retrieve tail gas and recycle, avoids the waste of material. This reaction system still includes gas-phase steel bottle 62 and gas mass flowmeter 66, and gas-phase steel bottle 62, gas mass flowmeter 66 and gas inlet 15 communicate in order, and gas-phase steel bottle 62 is arranged in providing the gaseous phase raw materials that gets into among the gas-liquid mixture reaction unit, according to the difference of reaction gaseous phase raw materials, can use air compressor machine or liquid oxygen tower etc. to provide the required gaseous phase raw materials of reaction, and gas mass flowmeter 66 is used for the input speed of accurate control gas raw materials entering reaction system. The reaction system also comprises a liquid phase raw material storage tank 63, a material beating pump 64 and a liquid mass flow meter 65, wherein the liquid phase raw material storage tank 63, the material beating pump 64, the liquid mass flow meter 65 and the liquid inlet 16 are sequentially communicated, and the liquid phase storage tank is used for storing liquid phase raw materials entering the gas-liquid mixing reaction device; the material-beating pump 64 is connected with the liquid mass flowmeter 65, and the material-beating pump 64 is used for conveying the raw materials in the liquid-phase storage tank to the gas-liquid mixing reaction device; the liquid mass flow meter 65 is connected to the gas-liquid mixing reaction device, and the liquid mass flow meter 65 is used for accurately controlling the feeding speed of the liquid phase raw material into the gas-liquid mixing reaction device. And, in this application, because gaseous phase raw materials and liquid phase raw materials when getting into gas-liquid mixture reaction unit, the reaction product can discharge through export 17, can reduce the required gas storage volume of gas-liquid mixture reaction unit like this, greatly reduce the danger coefficient of a large amount of aggregations of high-risk gas.

Further, the reaction system further includes a temperature detecting member 81, a temperature adjusting member 82, and a control member 83. The temperature detection member 81 is provided at the temperature measurement port 18 of the gas-liquid mixing reaction device, and the temperature detection member 81 can detect temperature changes at different positions of the gas-liquid mixing reaction device. The temperature adjusting assembly 82 is connected to the primary jacket 30 and the secondary jacket 50, and the temperature adjusting assembly 82 can adjust the temperature of the heat exchange medium in the jacket of the gas-liquid mixing reaction apparatus. The temperature adjusting component 82 comprises a first temperature control device 821 and a second temperature control device 822, the first temperature control device 821 can control the temperature of the heat exchange medium in the primary jacket 30 through an automatic adjusting valve, and the primary jacket 30 is heated by the high-temperature medium, so that the reaction system reaches the reaction temperature; the second temperature control device 822 can control the temperature of the heat exchange medium in the secondary jacket 50 through an automatic control valve, the secondary jacket 50 adopts a high-low temperature all-in-one machine to carry out oil bath temperature control, the secondary jacket 50 can be heated, and meanwhile, the heat emitted by the reaction of the lower end system can be removed in time. The control member 83 is electrically connected with the temperature detection member 81 and the temperature adjustment assembly 82 respectively, the control member 83 controls the temperature adjustment assembly 82 to adjust the temperature of the heat exchange medium according to the data detected by the temperature detection member 81, and the control member 83 can accurately control the temperature in the reaction system, so that the gas-liquid mixing reaction device can be smoothly carried out.

In the application, the reaction system adopts PLC automatic control, and the gas-liquid phase raw materials are accurately set according to the equivalent weight of the raw materials required by the reaction, so that compared with the centralized feeding of the raw materials in the batch preparation process, the method has the advantages of good safety, high control precision and stable product quality. By adopting the structure, the gas-liquid mixing reaction device can be accurately controlled in real time, the heat accumulation risk is reduced, and relatively stable reaction can be effectively promoted; and moreover, the condition that the temperature cannot be timely reduced when the reaction is out of control in the reaction process can be effectively avoided, and the material spraying accident caused by material boiling in a reaction system can be further avoided. Wherein, each set of reaction system can be used in parallel by a plurality of gas-liquid mixture reaction device or a plurality of gas-liquid mixture reaction device use in series, and the gas-liquid mixture reaction device quantity that links to each other can set up 1 to 20, and the staff can make up according to actual productivity demand is nimble.

The tail gas treatment assembly 70 includes a gas-liquid separator 71, a tail gas condensing unit 72, and a tail gas absorbing unit 73. The gas-liquid separator 71 has a material inlet, a tail gas outlet, and a material outlet, the material inlet is communicated with the outlet 17 of the gas-liquid mixing reaction device, and the material outlet is communicated with the inlet of the storage device 61. According to the arrangement, a product system obtained by the gas-liquid mixing reaction device enters the gas-liquid separator 71 from the outlet 17, and a liquid-phase product system enters the storage device 61 from the material outlet of the gas-liquid separator 71 and is transferred to downstream post-treatment operation or temporarily stored for standby application.

Wherein, a pressure control device is arranged between the outlet 17 and the gas-liquid separator 71, and the pressure control device can adjust the internal pressure of the gas-liquid mixing reaction device and monitor and control the internal pressure to be maintained at the pressure required by the reaction in real time. The tail gas condensing device 72 has a condensing inlet and a condensing outlet, and the condensing inlet is communicated with the tail gas outlet. The tail gas condensing unit 72 is used for condensing a liquid phase system carried in the tail gas, so that the liquid phase system flows back to the gas-liquid separator 71, and the product or the solvent is prevented from being discharged along with the tail gas. The tail gas absorption device 73 is communicated with the condensation outlet, and the tail gas absorption device 73 can absorb and dissolve exhausted gas, so that the pollution of the tail gas to the surrounding environment is avoided.

For a better understanding of the protocol of the present application, the results of comparing the reaction system of the present application with the batch-operated, plug-flow reaction apparatus experiments are shown below:

example 1:

the 2-fluoro-4-chlorotoluene and the catalyst are all put into a batch reaction device, a plug flow reaction device and the gas-liquid mixed reaction device for reaction, and the reaction results are as follows:

therefore, the conversion rate of the raw materials for gas-liquid mixing reaction is higher, and the product purity is higher. The continuous high-temperature oxygen oxidation synthesis device is suitable for replacing benzoic acid organic matters.

Example 2:

400g of m-xylene raw material and a catalyst are put into a batch reaction device and a gas-liquid mixing reaction device for reaction, and the reaction result is as follows:

from the above, the selectivity of the gas-liquid mixed reaction device is higher, and the overall yield is higher. The method is simultaneously suitable for preparing corresponding benzoic acid products by air oxidation of o-, m-and p-xylene, and the reaction effect has the same advantages compared with batch reaction devices.

It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the present application. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.

Unless specifically stated otherwise, the relative arrangement of the components and steps, the numerical expressions, and numerical values set forth in these embodiments do not limit the scope of the present invention. Meanwhile, it should be understood that the sizes of the respective portions shown in the drawings are not drawn in an actual proportional relationship for the convenience of description. Techniques, methods, and apparatus known to one of ordinary skill in the relevant art may not be discussed in detail but are intended to be part of the specification where appropriate. In all examples shown and discussed herein, any particular value should be construed as merely illustrative, and not limiting. Thus, other examples of the exemplary embodiments may have different values. It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be discussed further in subsequent figures.

In the description of the present invention, it should be understood that the directions or positional relationships indicated by the directional terms such as "front, back, upper, lower, left, right", "horizontal, vertical, horizontal" and "top, bottom", etc. are usually based on the directions or positional relationships shown in the drawings, and are only for convenience of description and simplification of the description, and in the case of not making a contrary explanation, these directional terms do not indicate and imply that the device or element referred to must have a specific direction or be constructed and operated in a specific direction, and therefore, should not be construed as limiting the scope of the present invention; the terms "inner and outer" refer to the inner and outer relative to the profile of the respective component itself.

For ease of description, spatially relative terms such as "over 8230," "upper surface," "above," and the like may be used herein to describe the spatial positional relationship of one device or feature to other devices or features as illustrated in the figures. It will be understood that the spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures. For example, if a device in the figures is turned over, devices described as "above" or "on" other devices or configurations would then be oriented "below" or "under" the other devices or configurations. Thus, the exemplary terms "at 8230; \8230; 'above" may include both orientations "at 8230; \8230;' above 8230; 'at 8230;' below 8230;" above ". The device may be otherwise variously oriented (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein interpreted accordingly.

It should be noted that the terms "first", "second", and the like are used to define the components, and are only used for convenience of distinguishing the corresponding components, and if not stated otherwise, the terms have no special meaning, and therefore, the scope of the present invention should not be construed as being limited.

The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims (10)

1. A gas-liquid mixing reaction apparatus, characterized by comprising:

the reactor comprises a shell (10), a gas inlet (15), a liquid inlet (16) and an outlet (17), wherein the shell (10) is provided with a primary mixing section (11), a primary reaction section (12), a secondary mixing section (13) and a secondary reaction section (14) which are sequentially communicated, the gas inlet (15) and the liquid inlet (16) are both communicated with the first section of the primary mixing section (11), and the outlet (17) is communicated with the tail end of the secondary reaction section (14);

the first gas-liquid distributor (20) is arranged in the primary mixing section (11), through holes are formed in the first gas-liquid distributor (20), and the opening rate of the first gas-liquid distributor (20) is 10% -50%;

the primary jacket (30) is arranged on the periphery of the shell (10) and positioned outside the primary reaction section (12), and the primary jacket (30) is used for heating a gas-liquid mixture in the primary reaction section (12);

the second gas-liquid distributor (40) is arranged in the secondary mixing section (13), and through holes are formed in the second gas-liquid distributor (40);

the secondary jacket (50) is arranged on the periphery of the shell (10) and positioned outside the secondary reaction section (14), and the secondary jacket (50) is used for heating the gas-liquid mixture of the secondary reaction section (14).

2. The gas-liquid mixing reaction device of claim 1, wherein the first gas-liquid distributor (20) has a mixing inlet, a mixing cavity and a mixing outlet, the mixing inlet is respectively communicated with the gas inlet (15) and the liquid inlet (16), the mixing inlet and the mixing outlet are respectively positioned at two ends of the first gas-liquid distributor (20), and the first gas-liquid distributor (20) is provided with a plurality of liquid outlet holes.

3. The gas-liquid mixing reaction device according to claim 1, wherein the first gas-liquid distributor (20) has an opening ratio of 30% to 40%.

4. The gas-liquid mixing reaction device according to claim 1, wherein the second gas-liquid distributor (40) has an opening rate of 30% to 70%.

5. The gas-liquid mixing reaction device according to claim 4, wherein the ratio of the height to the pore diameter of the first gas-liquid distributor (20) is in the range of 1 to 10.

6. The gas-liquid mixing reaction device according to claim 1, wherein a plurality of temperature measuring ports (18) are provided on the housing (10), the plurality of temperature measuring ports (18) are all communicated with the interior of the housing (10), at least one temperature measuring port (18) is provided near the first section of the primary reaction section (12), at least one temperature measuring port (18) is provided near the secondary mixing section (13), and at least one temperature measuring port (18) is provided near the end of the secondary reaction section (14).

7. The gas-liquid mixing reaction device according to claim 1, wherein an end plate (19) is detachably provided on the housing (10), the end plate (19) is provided near the primary mixing section (11), and the first gas-liquid distributor (20) is provided on the end plate (19).

8. A reaction system, comprising:

a gas-liquid mixing reaction apparatus according to any one of claims 1 to 7;

the storage device (61) is communicated with an outlet (17) of the gas-liquid mixing reaction device;

and the tail gas treatment component (70) is communicated with the outlet (17) of the gas-liquid mixing reaction device.

9. The reaction system of claim 8, further comprising:

the temperature detection piece (81) is arranged at a temperature measurement port (18) of the gas-liquid mixing reaction device;

the temperature adjusting assembly (82) is connected with the primary jacket (30) and the secondary jacket (50), and the temperature adjusting assembly (82) can adjust the temperature of a heat exchange medium in the jacket of the gas-liquid mixing reaction device;

and the control part (83) is respectively and electrically connected with the temperature detection part (81) and the temperature adjusting assembly (82), and the control part (83) controls the temperature adjusting assembly (82) to adjust the temperature of the heat exchange medium according to the data detected by the temperature detection part (81).

10. The reaction system of claim 8, wherein the tail gas treatment assembly (70) comprises:

the gas-liquid separator (71), the gas-liquid separator (71) has a material inlet, a tail gas outlet and a material outlet, the material inlet is communicated with the outlet (17) of the gas-liquid mixing reaction device, and the material outlet is communicated with the inlet of the material storage device (61);

a tail gas condensing unit (72), the tail gas condensing unit (72) having a condensing inlet and a condensing outlet, the condensing inlet in communication with the tail gas outlet;

and the tail gas absorption device (73) is communicated with the condensation outlet.

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