CN218501988U - Device for preparing 2, 4-diaminoanisole by continuous catalytic hydrogenation - Google Patents
Device for preparing 2, 4-diaminoanisole by continuous catalytic hydrogenation Download PDFInfo
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Abstract
The utility model relates to a device for preparing 2, 4-diaminoanisole by continuous catalytic hydrogenation, wherein a micro-mixing heat exchanger is provided with a gas material inlet, a liquid material inlet and a gas-liquid mixture outlet, a nitrogen input pipeline, a hydrogen input pipeline and a gas material inlet are respectively connected with corresponding ports on a three-way valve, and the liquid material inlet is connected with the liquid material input pipelineThen, a gas-liquid mixture outlet, the micro packed bed reactor and the gas-liquid separator are sequentially connected in series through pipelines; 2, 4-dinitroanisole is dissolved in organic solvent to prepare liquid material which is input through a liquid material input pipeline, a catalyst cavity and a heat exchange medium cavity are arranged inside the micro packed bed reactor, and Pd (OH) is arranged in the catalyst cavity 2 a/C catalyst. The utility model discloses possess the high-efficient mixing ability of gas-liquid and high-efficient ability of preheating, when ability accurate control reaction sequence and shortening reaction time, also improved reaction conversion and selectivity, whole process is simple more reliable.
Description
Technical Field
The utility model relates to the field of production and preparation of 2, 4-diaminoanisole, in particular to a device for preparing 2, 4-diaminoanisole by continuous catalytic hydrogenation.
Background
2, 4-diaminoanisole is an important organic synthesis intermediate, and is widely applied to the fields of fine chemicals such as dye and pigment, medicine, pesticide and the like.
2, 4-diaminoanisole is generally produced by the hydrogenation reduction of 2, 4-dinitroanisole, which contains two unsaturated nitro groups, and it is difficult to achieve complete conversion to 2, 4-diaminoanisole, since the conversion of the first nitro group (electron withdrawing group) to the amine group (electron donating group) reduces the electronic defects in the ring and prevents further reduction of the second nitro group.
The traditional industrial production technology of 2, 4-diamino anisole is as follows: raney nickel is used as a catalyst, hydrogen is used as a reducing agent, and a hydrogenation reduction reaction is carried out in an intermittent autoclave to obtain a product, but the Raney nickel is harsh in use condition and high in danger, and a certain amount of waste water and solid waste are generated in the reaction process, so that the environmental pollution is serious.
The research on the liquid-phase hydrogenation reaction of 2, 4-dinitroanisole of Chongxiaming et al [ Chongxiaming, chenxing, cheng-Bo-2, 4-dinitroanisole ] J. Fine chemical, 1997 (05): 43-45 ] adopts Pd/C catalyst to realize the hydrogenation reaction of 2, 4-dinitroanisole, but the reaction time of the process is long and the number of times of catalyst application is small.
Patent CN108218728A discloses a preparation method of 2, 4-diaminoanisole, which uses Pd/Al 2 O 3 The method is characterized in that kettle-type serial continuous hydrogenation is carried out for the catalyst, and the catalyst is separated by membrane filtration, so that the method has high production efficiency and product quality, but the catalyst needs to be continuously supplemented in the reaction process, and complicated and time-consuming sedimentation filtration operation is also needed.
Furthermore, many studies have shown that satisfactory results are difficult to achieve for the process of modifying aromatic dinitro compounds in a batch reactor using only a catalyst.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a device for preparing 2, 4-diaminoanisole by continuous catalytic hydrogenation, which utilizes a micro-mixing heat exchanger to realize the high-efficiency gas-liquid mixing capacity and the high-efficiency preheating capacity and utilizes a micro-packed bed reactor and Pd (OH) 2 The catalyst/C realizes the connection hydrogenation reaction, can accurately control the reaction process and shorten the reaction time, simultaneously improves the reaction conversion rate and selectivity, and has simpler and more reliable whole process.
The purpose of the utility model is realized through the following technical scheme:
a device for preparing 2, 4-diamino anisole by continuous catalytic hydrogenation comprises a nitrogen input pipeline, a hydrogen input pipeline, a three-way valve, a liquid material input pipeline, a micro-mixing heat exchanger, a micro-packed bed reactor and a gas-liquid separatorThe micro-mixing heat exchanger is provided with a gas material inlet, a liquid material inlet and a gas-liquid mixture outlet, the nitrogen input pipeline, the hydrogen input pipeline and the gas material inlet are respectively connected with corresponding ports on the three-way valve, the liquid material inlet is connected with the liquid material input pipeline, and the gas-liquid mixture outlet, the micro-packed bed reactor and the gas-liquid separator are sequentially connected in series through pipelines; 2, 4-dinitroanisole is dissolved in an organic solvent to prepare a liquid material which is input through the liquid material input pipeline, a catalyst cavity and a heat exchange medium cavity are arranged inside the micro packed bed reactor, the heat exchange medium cavity surrounds the catalyst cavity, and Pd (OH) is arranged in the catalyst cavity 2 a/C catalyst.
The micro-mixing heat exchanger is characterized in that a mixing channel and heat exchange media arranged around the mixing channel are arranged in the micro-mixing heat exchanger, the gas material inlet and the liquid material inlet are communicated with the input end of the mixing channel, and the output end of the mixing channel is communicated with the gas-liquid mixture outlet.
The mixing channel in the micro-mixing heat exchanger comprises a first mixing section and a second mixing section, wherein the first mixing section comprises a flow dividing unit and a converging unit which are arranged in a staggered mode, a first flow dividing block and a second flow dividing block are arranged in the second mixing section in a staggered mode, and the second flow dividing block is larger than the first flow dividing block.
The flow dividing unit comprises two flow dividing channels which are arranged in a diamond shape, and the first flow dividing block and the second flow dividing block are both circular; and a communicating channel is arranged in the micro-mixing heat exchanger, and the gas material inlet and the liquid material inlet are respectively communicated with the input end of the mixing channel through different communicating channels.
The micro-mixing heat exchanger is provided with a first heat exchange medium inlet and a first heat exchange medium outlet, and the first heat exchange medium inlet and the first heat exchange medium outlet are communicated with a cavity for containing heat exchange media in the micro-mixing heat exchanger.
The packed bed reactor one end is equipped with the reactor entry a little, and the other end is equipped with the reactor export, the first end in catalyst chamber with reactor access connection, just be equipped with first sieve in the first end, the second tip in catalyst chamber with reactor exit connection, just be equipped with the second sieve in the second end.
And a second heat exchange medium inlet and a second heat exchange medium outlet are arranged on the micro packed bed reactor, and the second heat exchange medium inlet and the second heat exchange medium outlet are communicated with the heat exchange medium cavity.
The input end of the nitrogen input pipeline is connected with a high-pressure nitrogen cylinder, the input end of the hydrogen input pipeline is connected with a high-pressure hydrogen cylinder, and gas circuit control ball valves are arranged on the nitrogen input pipeline and the hydrogen input pipeline.
And a gas mass flow controller and a pressure gauge are arranged on a connecting pipeline between the three-way valve and the micro-mixing heat exchanger, a high-pressure pump and a one-way valve are arranged on the liquid material input pipeline, and a back pressure valve is arranged on the gas-liquid separator.
Thermometers are arranged on a pipeline between the micro-mixing heat exchanger and the micro-packed bed reactor and a pipeline between the micro-packed bed reactor and the gas-liquid separator.
The utility model discloses an advantage does with positive effect:
1. the utility model discloses a micro-mixing heat exchanger possesses the high-efficient mixing ability of gas-liquid and high-efficient ability of preheating simultaneously, and high-efficient gas-liquid mixture enables material gas-liquid distribution even and avoids follow-up because the local overheat that the material mixing inhomogeneous leads to, and the high efficiency is preheated and is made the gas-liquid mixture material reach required temperature fast, shortens the time, in addition the utility model discloses the device adopts little packed bed reactor, has bigger gas-liquid solid three-phase area of contact and higher heat and mass transfer ability than conventional cauldron formula reactor, can more accurate control reaction to shorten reaction period.
2. The utility model adopts Pd (OH) 2 The catalyst has high activity, stable performance and high hydrogenation reaction selectivity, and the utility model is applied to the hydrogenation of 2, 4-dinitroanisole, and the conversion rate is 100 percent.
3. The utility model discloses in being fixed in little packed bed reactor with the catalyst, follow-up filtration operation that need not to realized the serialization hydrogenation, improved production efficiency, reduced intensity of labour. Meanwhile, the three wastes are not generated in the reaction process, thereby being beneficial to resource saving and environmental protection.
Drawings
Figure 1 is a schematic structural diagram of the present invention,
figure 2 is a schematic external view of the micro-hybrid heat exchanger of figure 1,
figure 3 is a schematic diagram of the internal structure of the micro-hybrid heat exchanger of figure 2,
FIG. 4 is a schematic external view of the micro packed bed reactor of FIG. 1,
fig. 5 is a schematic view of the internal structure of the micro packed bed reactor of fig. 4.
The system comprises a high-pressure nitrogen cylinder 1, a high-pressure hydrogen cylinder 2, a gas path control ball valve 3, a three-way valve 4, a gas mass flow controller 5, a pressure gauge 6, a high-pressure pump 7, a one-way valve 8, a micro-mixing heat exchanger 9, a gas material inlet 901, a liquid material inlet 902, a first heat exchange medium inlet 903, a first heat exchange medium outlet 904, a gas-liquid mixture outlet 905, a mixing channel 906, a flow dividing unit 9061, a converging unit 9062, a second flow dividing block 9063, a first flow dividing block 9064, a communicating channel 907, a thermometer 10, a micro-packed bed reactor 11, a reactor inlet 1101, a first sieve plate 1102, a second heat exchange medium inlet 1103, a second heat exchange medium outlet 1104, a second sieve plate 1105, a reactor outlet 1106, a back pressure valve 12 and a gas-liquid separator 13.
Detailed Description
The present invention will be described in detail with reference to the accompanying drawings.
As shown in fig. 1-5, the utility model discloses a nitrogen gas input pipeline, hydrogen input pipeline, three-way valve 4, liquid material input pipeline, micro-mixing heat exchanger 9, micro-packed bed reactor 11 and vapour and liquid separator 13, wherein as shown in fig. 2-3, micro-mixing heat exchanger 9 is equipped with gaseous material entry 901, liquid material entry 902 and gas-liquid mixture export 905, the inside mixing passage 906 that is equipped with of micro-mixing heat exchanger 9 with fill in heat transfer medium around mixing passage 906, gaseous material entry 901 and liquid material entry 902 all with mixing passage 906's input intercommunication, mixing passage 906's output with gas-liquid mixture export 905 intercommunication, as shown in fig. 1, nitrogen gas input pipeline, hydrogen input pipeline, gaseous material entry 901 respectively with the port that corresponds on the three-way valve 4 is connected, liquid material entry 902 with liquid material input pipeline connects, gas-liquid mixture export 905, micro-packed bed reactor 11 and vapour and liquid separator 13 establish ties through the pipeline in proper order.
As shown in fig. 3, the mixing channel 906 in the micro-mixing heat exchanger 9 includes a first mixing section and a second mixing section, wherein the first mixing section includes a flow dividing unit 9061 and a converging unit 9062 which are arranged in a staggered manner, in this embodiment, the flow dividing unit 9061 includes two flow dividing channels arranged in a diamond shape, and a material flows into the flow dividing unit 9061 and then is divided into two flows along different flow dividing channels, and then is converged again and flows into a single channel of the next converging unit 9062, so that continuous flow dividing and converging of the material are realized, and further material mixing is realized. Because first mixed section is the primary mixing of liquid material and gaseous material, consequently the utility model discloses a crisscross reposition of redundant personnel unit 9061 that sets up realizes the reposition of redundant personnel of two kinds of materials by a relatively large margin and assembles with assembling unit 9062, guarantees to mix fully.
As shown in fig. 3, a first shunting block 9064 and a second shunting block 9063 are arranged in the second mixing section in a staggered manner, in this embodiment, the first shunting block 9064 and the second shunting block 9063 are both circular, the diameter of the second shunting block 9063 is larger than that of the first shunting block 9064, and when a material passes through the first shunting block 9064 and the second shunting block 9063 when the second mixing section flows, the material sequentially flows through a gap between two sides of the first shunting block 9064 and a pipe wall of the second mixing section and a gap between two sides of the second shunting block 9063 and a pipe wall of the second mixing section, so that the material is continuously shunted and converged, and is further mixed. Because the material gets into in the second mixes the section after first mixing section intensive mixing, consequently the utility model discloses utilize first reposition of redundant personnel piece 9064 and second reposition of redundant personnel piece 9063 that the diameter is different to realize that the material is less range relatively simultaneously the range still changeable reposition of redundant personnel assemble to guarantee that the material mixes and abundant heat transfer in the second mixes section internal stability.
As shown in fig. 3, a communication channel 907 is disposed in the micro-hybrid heat exchanger 9, and the gas material inlet 901 and the liquid material inlet 902 are respectively communicated with the input end of the mixing channel 906 through different communication channels 907, and the communication channels 907 are disposed in the heat exchange medium.
As shown in fig. 2 to 3, a first heat exchange medium inlet 903 and a first heat exchange medium outlet 904 are provided on the micro-hybrid heat exchanger 9, and both the first heat exchange medium inlet 903 and the first heat exchange medium outlet 904 are communicated with a cavity for accommodating a heat exchange medium in the micro-hybrid heat exchanger 9. In this embodiment, the heat exchange medium is high-temperature water.
As shown in fig. 4 to 5, a catalyst chamber is arranged inside the micro packed bed reactor 11, and Pd (OH) is arranged in the catalyst chamber 2 /C catalyst, said Pd (OH) 2 In the/C catalyst, pd (OH) 2 7 percent of the catalyst, the carrier is spherical active carbon, the average grain diameter is 0.6mm, and the specific surface area of the catalyst is not less than 800m 2 /g。
As shown in fig. 4 to 5, one end of the micro packed bed reactor 11 is provided with a reactor inlet 1101, the other end is provided with a reactor outlet 1106, the first end of the catalyst cavity is connected to the reactor inlet 1101, the first end is provided with a first sieve plate 1102, the second end of the catalyst cavity is connected to the reactor outlet 1106, the second end is provided with a second sieve plate 1105, and the first sieve plate 1102 and the second sieve plate 1105 are used for preventing the catalyst from flowing out. As shown in fig. 1, the reactor inlet 1101 communicates with the gas-liquid mixture outlet 905 of the micro-mixing heat exchanger 9 through a pipe, and the reactor outlet 1106 communicates with the gas-liquid separator 13.
As shown in fig. 4 to 5, a heat exchange medium cavity is arranged in the micro packed bed reactor 11, the heat exchange medium cavity surrounds the catalyst cavity, a second heat exchange medium inlet 1103 and a second heat exchange medium outlet 1104 are arranged on the micro packed bed reactor 11, and the second heat exchange medium inlet 1103 and the second heat exchange medium outlet 1104 are both communicated with the heat exchange medium cavity.
As shown in fig. 1, the input end of the nitrogen input pipeline is connected with a high-pressure nitrogen cylinder 1, the output end of the nitrogen input pipeline is connected with a corresponding port of the three-way valve 4, the input end of the hydrogen input pipeline is connected with a high-pressure hydrogen cylinder 2, the output end of the hydrogen input pipeline is connected with a corresponding port of the three-way valve 4, and the nitrogen input pipeline and the hydrogen input pipeline are both provided with gas path control ball valves 3.
As shown in fig. 1, a gas mass flow controller 5 and a pressure gauge 6 are arranged on a connecting pipeline between the three-way valve 4 and the micro-mixing heat exchanger 9, the gas mass flow controller 5 and the pressure gauge 6 are used for controlling the flow and the pressure of a gas material input into the micro-mixing heat exchanger 9, and the gas mass flow controller 5 and the pressure gauge 6 are both known in the art and are commercially available products.
As shown in fig. 1, a high-pressure pump 7 and a check valve 8 are disposed on the liquid material input pipeline, wherein the high-pressure pump 7 is used for pumping the liquid material into the micro-mixing heat exchanger 9, the high-pressure pump 7 and the check valve 8 are both known in the art and are commercially available products, in this embodiment, 2, 4-dinitroanisole is dissolved in an organic solvent to prepare a liquid material, and the organic solvent may be tetrahydrofuran or ethyl acetate.
As shown in fig. 1, thermometers 10 are disposed on the pipeline between the micro-hybrid heat exchanger 9 and the micro-packed bed reactor 11 and the pipeline between the micro-packed bed reactor 11 and the gas-liquid separator 13 for detecting the temperature of the input or output material, and the thermometers 10 are well known in the art and are commercially available products.
As shown in fig. 1, a back pressure valve 12 is provided on the gas-liquid separator 13, and the back pressure valve 12 is a commercially available product and is well known in the art.
The utility model discloses a theory of operation does:
the utility model discloses during operation, each part is connected in order to order and Pd (OH) 2/C catalyst is filled in micro-packed bed reactor 11, then opens nitrogen gas input pipeline under the ordinary pressure, utilizes nitrogen gas to sweep the air in the pipeline and discharge, and makes the catalyst protect under the nitrogen atmosphere, and the inspection system leakproofness, and 2, 4-dinitroanisole is dissolved and is prepared into liquid material in the organic solvent, and will hold the container and the liquid material input tube coupling of liquid material, bear heat transfer medium's cavity then is connected with cold and hot circulation all-in-one through the pipeline respectively in micro-mixed heat exchanger 9 and the micro-packed bed reactor 11, cold and hot circulation all-in-one is the known technology in this field and purchases the product for the market, and it can set for heat transfer medium temperature, then opens nitrogen gas replacement in the nitrogen gas input pipeline realization system pipeline to set up backpressure valve 12 pressure values, then open hydrogen gas input pipeline and set up the flow parameter of gas quality flow controller 5, set for high-pressure pump 7 flow simultaneously, when cold and hot circulation all-in-one temperature reachs the settlement temperature, open high-pressure pump 7 input material to mix material input liquid material to micro-mix heat exchanger and to micro-mixed heat exchanger and realize that hydrogen flow controller 5 gets into the hydrogen reaction and the micro-mixed bed reactor 11 simultaneously, then the reaction of micro-mixed material reaction is carried out through the reaction heat exchanger, and the micro-mixed bed reactor together:
after the system had stabilized, a product sample was collected from the liquid outlet of the gas-liquid separator 13.
The Pd (OH) 2 Catalyst Pd (OH) 2 7 percent of the catalyst, the carrier is spherical active carbon, the average grain diameter is 0.6mm, and the specific surface area of the catalyst is not less than 800m 2 /g。
The following description is provided to illustrate a specific application of the present invention.
Application example 1
Connecting the device parts in sequence, pd (OH) 2 Filling a/C catalyst in a micro packed bed reactor 11, then opening a nitrogen input pipeline under normal pressure, blowing and discharging air in the pipeline by using nitrogen, protecting the catalyst in the nitrogen atmosphere, checking the tightness of the system, dissolving 2, 4-dinitroanisole in ethyl acetate to prepare a reaction solution with the concentration of 0.2mol/L, opening a cold-hot circulation all-in-one machine, setting the reaction temperature to be 60 ℃, and starting nitrogen inputThe pipeline realizes nitrogen replacement in the pipeline of the system, the pressure value of a back pressure valve 12 is set to be 2.0MPa, a hydrogen input pipeline is opened, the flow parameter of a gas mass flow controller 5 is set to be 50mL/min, the flow of a high-pressure pump 7 is set to be 0.5mL/min, the high-pressure pump 7 is opened when the temperature of the cold-hot circulation integrated machine reaches a set temperature of 60 ℃, the prepared liquid material is input into a micro-mixing heat exchanger 9 through a liquid material input pipeline, the micro-mixing heat exchanger 9 realizes material mixing and can realize preheating through a heat exchange medium, then the material enters a micro-packed bed reactor 11 for continuous hydrogenation reaction, and after the system is stable, a sample is collected from a liquid outlet of a gas-liquid separator 13.
After the reaction is finished, the catalyst and the reactor are flushed by methanol, the methanol is discharged by purging with nitrogen, and the catalyst is protected under the nitrogen atmosphere. The reaction product of the application example is analyzed by gas chromatography: the reaction conversion was 100% and the selectivity was 97.62%.
Claims (8)
1. A device for preparing 2, 4-diaminoanisole by continuous catalytic hydrogenation is characterized in that: the device comprises a nitrogen input pipeline, a hydrogen input pipeline, a three-way valve (4), a liquid material input pipeline, a micro-mixing heat exchanger (9), a micro-packed bed reactor (11) and a gas-liquid separator (13), wherein the micro-mixing heat exchanger (9) is provided with a gas material inlet (901), a liquid material inlet (902) and a gas-liquid mixture outlet (905), the nitrogen input pipeline, the hydrogen input pipeline and the gas material inlet (901) are respectively connected with corresponding ports on the three-way valve (4), the liquid material inlet (902) is connected with the liquid material input pipeline, and the gas-liquid mixture outlet (905), the micro-packed bed reactor (11) and the gas-liquid separator (13) are sequentially connected in series through pipelines; 2, 4-dinitroanisole is dissolved in an organic solvent to prepare a liquid material which is input through the liquid material input pipeline, a catalyst cavity and a heat exchange medium cavity are arranged inside the micro packed bed reactor (11), the heat exchange medium cavity surrounds the catalyst cavity, and Pd (OH) is arranged in the catalyst cavity 2 A catalyst;
a mixing channel (906) and a heat exchange medium arranged around the mixing channel (906) are arranged in the micro-mixing heat exchanger (9), the gas material inlet (901) and the liquid material inlet (902) are both communicated with the input end of the mixing channel (906), and the output end of the mixing channel (906) is communicated with the gas-liquid mixture outlet (905);
a mixing channel (906) in the micro-mixing heat exchanger (9) comprises a first mixing section and a second mixing section, wherein the first mixing section comprises a flow dividing unit (9061) and a converging unit (9062) which are arranged in a staggered mode, a first flow dividing block (9064) and a second flow dividing block (9063) are arranged in the second mixing section in a staggered mode, and the second flow dividing block (9063) is larger than the first flow dividing block (9064).
2. The apparatus for preparing 2, 4-diaminoanisole by continuous catalytic hydrogenation according to claim 1, characterized in that: the flow dividing unit (9061) comprises two flow dividing channels which are arranged in a rhombic shape, and the first flow dividing block (9064) and the second flow dividing block (9063) are both circular; a communicating channel (907) is arranged in the micro-mixing heat exchanger (9), and the gas material inlet (901) and the liquid material inlet (902) are respectively communicated with the input end of the mixing channel (906) through different communicating channels (907).
3. The apparatus for preparing 2, 4-diaminoanisole by continuous catalytic hydrogenation according to claim 1, characterized in that: and a first heat exchange medium inlet (903) and a first heat exchange medium outlet (904) are arranged on the micro-mixing heat exchanger (9), and the first heat exchange medium inlet (903) and the first heat exchange medium outlet (904) are communicated with a cavity for bearing heat exchange media in the micro-mixing heat exchanger (9).
4. The apparatus for preparing 2, 4-diaminoanisole by continuous catalytic hydrogenation according to claim 1, characterized in that: one end of the micro packed bed reactor (11) is provided with a reactor inlet (1101), the other end of the micro packed bed reactor is provided with a reactor outlet (1106), the first end part of the catalyst cavity is connected with the reactor inlet (1101), a first sieve plate (1102) is arranged in the first end part, the second end part of the catalyst cavity is connected with the reactor outlet (1106), and a second sieve plate (1105) is arranged in the second end part.
5. The apparatus for preparing 2, 4-diaminoanisole by continuous catalytic hydrogenation according to claim 1, characterized in that: and a second heat exchange medium inlet (1103) and a second heat exchange medium outlet (1104) are arranged on the micro packed bed reactor (11), and the second heat exchange medium inlet (1103) and the second heat exchange medium outlet (1104) are communicated with the heat exchange medium cavity.
6. The apparatus for preparing 2, 4-diaminoanisole by continuous catalytic hydrogenation according to claim 1, characterized in that: the input end of the nitrogen input pipeline is connected with a high-pressure nitrogen cylinder (1), the input end of the hydrogen input pipeline is connected with a high-pressure hydrogen cylinder (2), and gas path control ball valves (3) are arranged on the nitrogen input pipeline and the hydrogen input pipeline.
7. The apparatus for preparing 2, 4-diaminoanisole by continuous catalytic hydrogenation according to claim 1, characterized in that: the device is characterized in that a gas mass flow controller (5) and a pressure gauge (6) are arranged on a connecting pipeline between the three-way valve (4) and the micro-mixing heat exchanger (9), a high-pressure pump (7) and a one-way valve (8) are arranged on the liquid material input pipeline, and a back pressure valve (12) is arranged on the gas-liquid separator (13).
8. The apparatus for preparing 2, 4-diaminoanisole by continuous catalytic hydrogenation according to claim 1, characterized in that: thermometers (10) are arranged on a pipeline between the micro-mixing heat exchanger (9) and the micro-packed bed reactor (11) and a pipeline between the micro-packed bed reactor (11) and the gas-liquid separator (13).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202221948066.XU CN218501988U (en) | 2022-07-27 | 2022-07-27 | Device for preparing 2, 4-diaminoanisole by continuous catalytic hydrogenation |
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| CN202221948066.XU CN218501988U (en) | 2022-07-27 | 2022-07-27 | Device for preparing 2, 4-diaminoanisole by continuous catalytic hydrogenation |
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