CN219689338U - Hydrogenation system for producing hydrogen peroxide by anthraquinone process - Google Patents
Hydrogenation system for producing hydrogen peroxide by anthraquinone process Download PDFInfo
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- CN219689338U CN219689338U CN202320782350.2U CN202320782350U CN219689338U CN 219689338 U CN219689338 U CN 219689338U CN 202320782350 U CN202320782350 U CN 202320782350U CN 219689338 U CN219689338 U CN 219689338U
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 169
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 title claims abstract description 46
- PYKYMHQGRFAEBM-UHFFFAOYSA-N anthraquinone Natural products CCC(=O)c1c(O)c2C(=O)C3C(C=CC=C3O)C(=O)c2cc1CC(=O)OC PYKYMHQGRFAEBM-UHFFFAOYSA-N 0.000 title claims abstract description 23
- 150000004056 anthraquinones Chemical class 0.000 title claims abstract description 23
- 238000000034 method Methods 0.000 title claims abstract description 22
- 230000008569 process Effects 0.000 title claims abstract description 19
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 74
- 239000001257 hydrogen Substances 0.000 claims abstract description 74
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 74
- 239000002101 nanobubble Substances 0.000 claims abstract description 64
- 239000012224 working solution Substances 0.000 claims abstract description 44
- 239000003054 catalyst Substances 0.000 claims abstract description 18
- 239000007789 gas Substances 0.000 claims description 29
- 238000003756 stirring Methods 0.000 claims description 27
- 239000012530 fluid Substances 0.000 claims description 23
- 229910052751 metal Inorganic materials 0.000 claims description 20
- 239000002184 metal Substances 0.000 claims description 20
- 241000736911 Turritella communis Species 0.000 claims description 19
- 239000011148 porous material Substances 0.000 claims description 19
- 239000007788 liquid Substances 0.000 claims description 18
- 238000004519 manufacturing process Methods 0.000 claims description 14
- 230000009471 action Effects 0.000 abstract description 9
- 239000000203 mixture Substances 0.000 abstract description 9
- 230000005484 gravity Effects 0.000 abstract description 5
- 238000006276 transfer reaction Methods 0.000 abstract description 5
- 239000012071 phase Substances 0.000 description 20
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 6
- 239000007791 liquid phase Substances 0.000 description 5
- PCFMUWBCZZUMRX-UHFFFAOYSA-N 9,10-Dihydroxyanthracene Chemical compound C1=CC=C2C(O)=C(C=CC=C3)C3=C(O)C2=C1 PCFMUWBCZZUMRX-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 229910052763 palladium Inorganic materials 0.000 description 3
- 238000010008 shearing Methods 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 230000004075 alteration Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Abstract
The utility model relates to a hydrogenation system for producing hydrogen peroxide by an anthraquinone process; the device comprises a first-stage hydrogenation tower and a second-stage hydrogenation tower, wherein an inlet of the first-stage hydrogenation tower is connected with a first-stage preposed micro-nano bubble premixer, and an outlet of the first-stage hydrogenation tower is connected with an inlet of the second-stage hydrogenation tower through a second-stage preposed micro-nano bubble premixer; the front parts of the primary hydrogenation tower and the secondary hydrogenation tower are respectively provided with a front micro-nano bubble premixer so as to realize the premixing of hydrogen and working solution; when the hydrogen and the working solution are premixed into a mixture, the mixture enters a corresponding hydrogenation tower, and the mixture flows from top to bottom in the hydrogenation tower under the action of gravity, so that the mixture contacts a catalyst bed layer to carry out mass transfer reaction, and the characteristic of improving the efficiency of a hydrogenation system is achieved.
Description
Technical Field
The utility model relates to the technical field of hydrogen peroxide production, in particular to a hydrogenation system for anthraquinone process hydrogen peroxide production.
Background
The technology for producing hydrogen peroxide by anthraquinone method mainly comprises a hydrogenation system, an oxidation system, an extraction system and a post-treatment system. In the hydrogenation system, anthraquinone in the working solution is used as a carrier to complete hydrogenation reaction of anthraquinone to generate anthrahydroquinone, and then the anthrahydroquinone enters the oxidation system to complete reaction of anthrahydroquinone and oxygen to generate hydrogen peroxide. The efficiency of the hydrogenation system is critical to overall plant capacity and consumption control. In the original process, working solution and hydrogen enter a hydrogenation tower respectively, and gas-liquid two phases (hydrogen and working solution) in the hydrogenation tower carry out mass transfer reaction of anthraquinone hydrogenation under the action of a palladium catalyst, but the efficiency of a hydrogenation system is low due to the fact that the reaction is influenced by the contact area of gas, liquid and solid phases and the mass transfer effect, and the production capacity of the whole device is insufficient due to the fact that the hydrogenation efficiency is low.
Disclosure of Invention
The utility model aims to provide a hydrogenation system for producing hydrogen peroxide by an anthraquinone process, which solves the problems in the prior art.
In order to achieve the above purpose, the present utility model provides the following technical solutions:
a hydrogenation system for producing hydrogen peroxide by an anthraquinone method comprises a primary hydrogenation tower and a secondary hydrogenation tower, wherein an inlet of the primary hydrogenation tower is connected with a primary preposed micro-nano bubble premixer, and an outlet of the primary hydrogenation tower is connected with an inlet of the secondary hydrogenation tower through the secondary preposed micro-nano bubble premixer.
The beneficial effects of the utility model are as follows: in the utility model, the front parts of the primary hydrogenation tower and the secondary hydrogenation tower are respectively provided with a prepositive micro-nano bubble premixer so as to realize the premixing of hydrogen and working solution; when the hydrogen and the working solution are premixed into a mixture, the mixture enters a corresponding hydrogenation tower, and the mixture flows from top to bottom in the hydrogenation tower under the action of gravity, so that the mixture contacts a catalyst bed layer to carry out mass transfer reaction, and the characteristic of improving the efficiency of a hydrogenation system is achieved.
Preferably, the first-stage front micro-nano bubble premixer and the second-stage front micro-nano bubble premixer have the same structure; the prepositive micro-nano bubble premixer comprises a shell, wherein a hydrogen pipeline and a working solution pipeline are arranged at the lower part of the shell, a gas-liquid mixing outlet pipeline is arranged at the upper part of the shell, the number of the hydrogen pipelines is several, the tail end inlets of the hydrogen pipelines are arranged along the tangential direction of the outer wall of the shell, and metal micro-pore plates are arranged at the tail end inlets of the hydrogen pipelines. According to the utility model, the tail end inlet of the hydrogen pipeline is arranged along the tangential direction of the outer wall of the shell and the metal micro-pore plate, so that the hydrogen is dispersed to form micro-bubbles after passing through the metal micro-pore plate, and the micro-bubbles are moved along the direction of the inner wall of the shell, so that the purposes of reducing the breakage of the micro-bubbles and meeting the better fusion of the working solution and the hydrogen are achieved.
Preferably, micropores are uniformly distributed on the metal microporous plate, and the pore diameter of the micropores is 10 nm-20 mu m. By arranging the micropores and limiting the pore diameter of the micropores, the limitation of the diameter range of the bubbles can be realized, and the diameter range of the bubbles is 10 nm-20 mu m, so that the purpose of dividing the bubbles into micro-nano bubbles and facilitating later-stage full mixing is achieved.
Preferably, the top of casing is equipped with agitator motor, and agitator motor's (mixing) shaft extends to inside the casing, and the end of (mixing) shaft is equipped with stirring vane. The stirring device is mainly used for being matched with the metal microporous plate and arranged at the tail end inlet of the hydrogen pipeline along the tangential direction of the outer wall of the shell, so that the working solution of high-speed rotational flow in the micro-nano bubbles is sheared and taken away and enters the liquid phase, and the working solution and the micro-nano bubbles are fully mixed in the shell.
Preferably, an ultrasonic generator is arranged at the bottom of the inner part of the shell. Through set up supersonic generator in leading micro-nano bubble pre-mixer, can assist the inside rotatory stirring vane of high speed of casing and disperse the hydrogen into micro-nano bubble to improve the mixing efficiency of working solution and micro-nano bubble.
Preferably, the hydrogen pipelines are uniformly distributed on the outer circumference of the shell.
Preferably, the first-stage hydrogenation tower and the second-stage hydrogenation tower have the same structure;
the hydrogenation tower comprises a hydrogenation tower shell, wherein the lower part of the hydrogenation tower shell is provided with a working fluid outlet, the upper part of the hydrogenation tower shell is provided with a working fluid inlet, the top of the hydrogenation tower shell is provided with a gas phase outlet, and the inside of the hydrogenation tower shell is provided with two catalyst beds.
Preferably, the gas-liquid mixing outlet pipeline of the primary preposed micro-nano bubble premixer is connected with the working solution inlet of the primary hydrogenation tower, the working solution outlet of the primary hydrogenation tower is connected with the working solution pipeline of the secondary preposed micro-nano bubble premixer through an intermediate hydrogenation pump and an intermediate hydrogenation liquid cooler, and the gas-liquid mixing outlet pipeline of the secondary preposed micro-nano bubble premixer is connected with the working solution inlet of the secondary hydrogenation tower; the working solution outlet of the secondary hydrogenation tower is connected with the subsequent working section through a hydrogenation pump.
Preferably, the gas phase outlet of the secondary hydrogenation tower is connected with the gas phase inlet of the primary hydrogenation tower through a pipeline, and the gas phase outlet of the primary hydrogenation tower is communicated with the atmosphere. Through the arrangement, redundant hydrogen in the secondary hydrogenation tower enters the primary hydrogenation tower, so that the recycling of the hydrogen is realized, and the hydrogenation efficiency in the primary hydrogenation tower can be improved.
Preferably, the gas phase inlet of the primary hydrogenation tower is arranged on the outer wall of the hydrogenation tower shell corresponding to the position between the two catalyst beds.
The utility model aims to improve the hydrogenation efficiency of the hydrogenation system so as to achieve the aim of improving the hydrogen peroxide yield; the utility model ensures that the contact of the hydrogen and the working solution adopts a pre-mixing mode, and the characteristic that the overflowed hydrogen in the secondary hydrogenation tower enters the primary hydrogenation tower for re-mixing can be utilized in the later stage, so as to solve the problem of low hydrogenation efficiency caused by directly mixing the hydrogen and the working solution in the hydrogenation tower in the prior art; the utility model includes the following technical means that 1, micro-nano bubbles are formed by dividing hydrogen into micro-nano bubbles by micro holes uniformly distributed on a metal micro-pore plate, and the micro-nano bubbles are dispersed in working solution by arranging pressurized gas and a tail end inlet of a hydrogen pipeline along the tangential direction of the outer wall of a shell; 2. and 3, utilizing the stirring device to enable the stirring blade to rotate at a high speed, so as to accelerate the mixing of the working solution and the micro-nano bubbles, and utilizing the ultrasonic generator to assist the stirring blade rotating at a high speed in the shell and dispersing hydrogen into micro-nano bubbles, so as to improve the mixing efficiency of the working solution and the micro-nano bubbles. The arrangement can effectively improve the mixing effect of the working solution and the hydrogen so as to achieve the purpose of fully mixing the working solution and the hydrogen before entering the hydrogenation tower and improving the hydrogenation efficiency; in addition, the utility model also enables redundant hydrogen in the secondary hydrogenation tower to enter the primary hydrogenation tower, thereby realizing the reutilization of the hydrogen and improving the hydrogenation efficiency in the primary hydrogenation tower; has the advantages of improving the efficiency of the hydrogenation system, improving the production capacity of hydrogen peroxide and reducing the hydrogen consumption.
Drawings
Fig. 1 is a schematic structural view of the present utility model.
Fig. 2 is a schematic structural diagram of a pre-micro-nano bubble premixer according to the present utility model.
FIG. 3 is a schematic view of the hydrogen pipeline end inlet and the shell according to the present utility model.
FIG. 4 is a schematic diagram of the structure of the hydrogenation column of the present utility model.
FIG. 5 is a schematic diagram of a metal microplate according to the present utility model.
In the figure: 1. a first stage hydrogenation tower; 2. a secondary hydrogenation tower; 3. a first-stage prepositioned micro-nano bubble premixer; 4. a second-stage prepositioned micro-nano bubble premixer; 5. an intermediate hydrogenation liquid cooler; 6. an intermediate hydrogenation pump; 7. a hydrogenation pump; 8. a catalyst bed; 9. stirring blades; 10. a hydrogen pipe; 11. a housing; 12. a working fluid pipe; 13. a gas-liquid mixing outlet pipe; 14. a metal microplate; 15. a stirring motor; 16. a stirring shaft; 17. an ultrasonic generator; 18. a working fluid outlet; 19. a working fluid inlet; 20. a gas phase outlet; 21. a subsequent working section; 22. and a gas phase inlet.
Detailed Description
The technical solutions in the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model.
Referring to fig. 1, a hydrogenation system for producing hydrogen peroxide by an anthraquinone process comprises a primary hydrogenation tower 1 and a secondary hydrogenation tower 2, wherein the inlet of the primary hydrogenation tower 1 is connected with a primary preposed micro-nano bubble premixer 3, and the outlet of the primary hydrogenation tower 1 is connected with the inlet of the secondary hydrogenation tower 2 through a secondary preposed micro-nano bubble premixer 4. According to the utility model, the preposed micro-nano bubble premixer 4 is adopted to realize the mixing of hydrogen and working solution, and the mixture enters the corresponding hydrogenation tower on the basis of the mixing, and flows from top to bottom in the hydrogenation tower under the action of gravity, so that the catalyst bed is contacted to carry out mass transfer reaction, and the characteristic of improving the efficiency of a hydrogenation system is achieved; the mode is different from the traditional technology that hydrogen is adopted to directly enter the hydrogenation tower, so that gas phase (hydrogen), liquid phase (working solution) and solid phase (catalyst in a catalyst bed) are in three-phase contact, the efficiency of mass transfer reaction is higher, and the characteristics of improving the hydrogenation efficiency and further improving the hydrogen peroxide yield are achieved.
Further, referring to fig. 2 and 3, the first stage front micro-nano bubble premixer 3 and the second stage front micro-nano bubble premixer 4 have the same structure; the prepositive micro-nano bubble premixer comprises a shell 11, wherein a hydrogen pipeline 10 and a working fluid pipeline 12 are arranged at the lower part of the shell 11, a gas-liquid mixing outlet pipeline 13 is arranged at the upper part of the shell 11, the number of the hydrogen pipelines 10 is several, the tail end inlets of the hydrogen pipelines 10 are arranged along the tangential direction of the outer wall of the shell 11, and a metal micro-pore plate 14 is arranged at the tail end inlet of the hydrogen pipeline 10. The front end of the hydrogen pipeline 10 is connected with a hydrogen gas source, the hydrogen gas source can comprise a hydrogen storage tank, a hydrogen pipeline, a hydrogen generating device and the like, hydrogen enters the metal micro-pore plate 14 through the hydrogen pipeline 10 under the condition of pressure, micro-nano bubbles are cut into micro-nano bubbles by micro-pores on the metal micro-pore plate 14 and are mixed with working fluid along the inner wall of the shell 11, and the arrangement can realize the full mixing of the micro-nano bubbles and the working fluid under the condition of reducing the breakage rate of the micro-nano bubbles.
Further, referring to fig. 5, micropores are uniformly distributed on the metal microporous plate 14, and the pore diameter of the micropores is 10nm to 20 μm. According to the utility model, the diameter of the micro-nano bubbles is limited by arranging the pore diameter of the micropores, and the micro-nano bubbles can be better dispersed in the working solution and can be reduced in loss of hydrogen by limiting the diameter of the micro-nano bubbles, and the purpose of fully fusing the micro-nano bubbles and the working solution is realized.
Further, referring to fig. 1 and 2, a stirring motor 15 is disposed at the top of the housing 11, a stirring shaft 16 of the stirring motor 15 extends into the housing 11, and a stirring blade 9 is disposed at the end of the stirring shaft 16. In the utility model, preferably, on the premise of starting the stirring device, the stirring blade 9 drives the working solution to rotate at a high speed, and the micro-nano bubbles are dispersed and fully mixed under the shearing action of the high-speed rotational flow working solution.
Further, referring to fig. 1 and 2, an ultrasonic generator 17 is provided at the bottom of the housing 11. Through setting up supersonic generator in leading micro-nano bubble pre-mixer, can assist the inside rotatory stirring vane 9 of high speed of casing 11 and disperse the hydrogen into micro-nano bubble to improve the mixing efficiency of working solution and micro-nano bubble.
Further, referring to fig. 3, the plurality of hydrogen pipes 10 are uniformly distributed on the outer circumference of the housing 11. Preferably, the number of the hydrogen pipelines 10 is four, and the hydrogen pipelines are uniformly distributed on the outer circumference of the shell 11.
Further, referring to fig. 1 and 4, the first-stage hydrogenation tower 1 and the second-stage hydrogenation tower 2 have the same structure; the hydrogenation tower comprises a hydrogenation tower shell, wherein a working fluid outlet 18 is formed in the lower portion of the hydrogenation tower shell, a working fluid inlet 19 is formed in the upper portion of the hydrogenation tower shell, a gas phase outlet 20 is formed in the top of the hydrogenation tower shell, and two catalyst beds 8 are arranged in the hydrogenation tower shell.
Further, referring to fig. 1 and 4, the gas-liquid mixing outlet pipe 13 of the primary front micro-nano bubble premixer is connected with the working solution inlet 19 of the primary hydrogenation tower, the working solution outlet 18 of the primary hydrogenation tower is connected with the working solution pipe 12 of the secondary front micro-nano bubble premixer through the intermediate hydrogenation pump 6 and the intermediate hydrogenation liquid cooler 5, and the gas-liquid mixing outlet pipe 13 of the secondary front micro-nano bubble premixer is connected with the working solution inlet 19 of the secondary hydrogenation tower; the working fluid outlet 18 of the secondary hydrogenation tower is connected with the subsequent working section 21 through the hydrogenation pump 7.
Further, referring to fig. 1, the gas phase outlet 20 of the secondary hydrogenation tower is connected to the gas phase inlet 22 of the primary hydrogenation tower 1 through a pipe, and the gas phase outlet 20 of the primary hydrogenation tower is connected to the atmosphere. The gas accumulated in the hydrogenation tower to a certain concentration can influence the safe operation of the hydrogenation tower; the tops of the primary hydrogenation tower 1 and the secondary hydrogenation tower 2 are respectively provided with a gas emptying pipeline, and the risks are avoided in a regular emptying mode in normal production; however, the above way can cause waste of hydrogen, and the content of hydrogen in the discharged air is generally more than or equal to 75%; the technical scheme of the utility model is that the gas phase outlet 20 of the secondary hydrogenation tower is led into the primary hydrogenation tower 1 through a pipeline, thereby realizing the reuse of hydrogen and improving the hydrogenation efficiency of the primary hydrogenation tower 1, and the hydrogen is discharged from the primary hydrogenation tower 1 in the same way.
Further, referring to fig. 1, the gas phase inlet 22 of the first-stage hydrogenation tower 1 is disposed on the outer wall of the hydrogenation tower shell corresponding to the space between the two catalyst beds 8.
The working principle of the utility model is as follows: the working solution treated by the post-treatment process enters the shell 11 of the primary preposed micro-nano bubble premixer 3 through the working solution pipeline 12, the stirring motor 15 is started and drives the stirring blade 9 to rotate through the stirring shaft 16, and the working solution is in a high-speed rotation state under the action of the stirring blade 9; the hydrogen with the pressure of 0.5Mpa from a hydrogen source enters a shell 11 through a plurality of hydrogen pipelines 10 and metal micro-pore plates 14, pressurized hydrogen passes through the metal micro-pore plates 14 to form micro-bubbles, the micro-bubbles are taken away by a rotational flow working fluid to enter a liquid phase to form micro-nano bubbles with the diameter of 10 nm-20 mu m, the micro-nano bubbles pass through the high-speed rotational flow of the working fluid, the gas and hydraulic shearing of the metal micro-pore pipes and the like, the fully mixed hydrogen and the working fluid enter a first-stage hydrogenation tower 1 through a gas-liquid mixing outlet pipeline 13, the hydrogen contacts with palladium catalyst in a catalyst bed layer under the action of gravity and generates anthraquinone hydrogenation reaction, the reacted material enters a second-stage front-stage micro-nano bubble premixer 2 through a working fluid outlet 18 of the first-stage hydrogenation tower, an intermediate hydrogenation pump 6, an intermediate hydrogenation liquid cooler 5 and a working fluid pipeline 12 of the second-stage front-stage micro-nano bubble premixer, and the stirring motor 15 is started and drives a stirring blade 9 to rotate through a stirring shaft 16, and the working fluid is in a high-speed rotation state under the action of the stirring blade 9; the method comprises the steps that 0.5Mpa hydrogen from a hydrogen source enters a shell 11 through a plurality of hydrogen pipelines 10 and metal micro-pore plates 14, pressurized hydrogen passes through the metal micro-pore plates 14 to form micro-bubbles, the micro-bubbles are taken away by a rotational flow working fluid flow and enter a liquid phase to form micro-nano bubbles with the diameter of 10 nm-20 mu m, the micro-nano bubbles pass through the high-speed rotational flow of the working fluid, the gas and hydraulic shearing of the metal micro-pore pipes and the like, the fully mixed hydrogen and the working fluid enter a secondary hydrogenation tower 2 through a gas-liquid mixing outlet pipeline 13, the hydrogen contacts with a palladium catalyst in a catalyst bed layer under the action of gravity and undergoes anthraquinone hydrogenation reaction, and reacted materials enter a subsequent working section 21 through a hydrogenation pump, wherein the subsequent working section 21 is a subsequent oxidation, extraction and other systems; in the running process, the ultrasonic generator 17 can be started to promote the dispersion and mixing of the hydrogen and the working solution; meanwhile, the preposed micro-nano bubble premixer can bring part of hydrogen into the hydrogenation tower, the gas phase outlet 20 of the secondary hydrogenation tower is connected with the gas phase inlet 22 of the primary hydrogenation tower 1 through a pipeline, the gas phase outlet 20 of the primary hydrogenation tower is communicated with the atmosphere, and the gas phase inlet 22 of the primary hydrogenation tower 1 is arranged on the outer wall of the corresponding hydrogenation tower shell between the two catalyst beds 8; the arrangement can realize recycling of the hydrogen, and improves the hydrogenation efficiency of the first-stage hydrogenation tower 1 while improving the utilization rate of the hydrogen; the high-speed rotation in the present utility model means that the rotation speed of the stirring blade 9 is 8000 to 10000 rpm.
Although embodiments of the present utility model have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the utility model, the scope of which is defined in the appended claims and their equivalents.
Claims (10)
1. A hydrogenation system for producing hydrogen peroxide by an anthraquinone process, comprising a primary hydrogenation tower (1) and a secondary hydrogenation tower (2), and being characterized in that: the inlet of the primary hydrogenation tower (1) is connected with the primary preposed micro-nano bubble premixer (3), and the outlet of the primary hydrogenation tower (1) is connected with the inlet of the secondary hydrogenation tower (2) through the secondary preposed micro-nano bubble premixer (4).
2. A hydrogenation system for the production of hydrogen peroxide by the anthraquinone process according to claim 1, characterized in that: the primary preposed micro-nano bubble premixer (3) and the secondary preposed micro-nano bubble premixer (4) have the same structure;
the prepositive micro-nano bubble premixer comprises a shell (11), a hydrogen pipeline (10) and a working fluid pipeline (12) are arranged at the lower part of the shell (11), a gas-liquid mixing outlet pipeline (13) is arranged at the upper part of the shell (11),
the hydrogen pipelines (10) are a plurality of, the tail end inlets of the hydrogen pipelines (10) are arranged along the tangential direction of the outer wall of the shell (11), and the metal micro-pore plates (14) are arranged at the tail end inlets of the hydrogen pipelines (10).
3. A hydrogenation system for the production of hydrogen peroxide by the anthraquinone process according to claim 2, characterized in that: micropores are uniformly distributed on the metal microporous plate (14), and the aperture of the micropores is 10 nm-20 mu m.
4. A hydrogenation system for the production of hydrogen peroxide by the anthraquinone process according to claim 2 or 3, characterized in that: the top of casing (11) is equipped with agitator motor (15), and agitator motor (15) stirring axle (16) extend to casing (11) inside, and agitator blade (9) are equipped with at the end of agitator axle (16).
5. A hydrogenation system for anthraquinone process hydrogen peroxide production, as set forth in claim 4, wherein: an ultrasonic generator (17) is arranged at the bottom of the inside of the shell (11).
6. A hydrogenation system for the production of hydrogen peroxide by the anthraquinone process according to claim 2, characterized in that: the hydrogen pipelines (10) are uniformly distributed on the outer circumference of the shell (11).
7. A hydrogenation system for the production of hydrogen peroxide by the anthraquinone process according to claim 2, characterized in that: the primary hydrogenation tower (1) and the secondary hydrogenation tower (2) have the same structure;
the hydrogenation tower comprises a hydrogenation tower shell, a working fluid outlet (18) is arranged at the lower part of the hydrogenation tower shell, a working fluid inlet (19) is arranged at the upper part of the hydrogenation tower shell, a gas phase outlet (20) is arranged at the top of the hydrogenation tower shell, and two catalyst beds (8) are arranged in the hydrogenation tower shell.
8. A hydrogenation system for anthraquinone process hydrogen peroxide production, as set forth in claim 7, characterized in that: the gas-liquid mixing outlet pipeline (13) of the primary front micro-nano bubble premixer is connected with the working solution inlet (19) of the primary hydrogenation tower, the working solution outlet (18) of the primary hydrogenation tower is connected with the working solution pipeline (12) of the secondary front micro-nano bubble premixer through the intermediate hydrogenation pump (6) and the intermediate hydrogenation liquid cooler (5), and the gas-liquid mixing outlet pipeline (13) of the secondary front micro-nano bubble premixer is connected with the working solution inlet (19) of the secondary hydrogenation tower; the working solution outlet (18) of the secondary hydrogenation tower is connected with the subsequent working section (21) through a hydrogenation pump (7).
9. A hydrogenation system for anthraquinone process hydrogen peroxide production, as set forth in claim 7, characterized in that: the gas phase outlet (20) of the secondary hydrogenation tower is connected with the gas phase inlet (22) of the primary hydrogenation tower (1) through a pipeline, and the gas phase outlet (20) of the primary hydrogenation tower is communicated with the atmosphere.
10. A hydrogenation system for the production of hydrogen peroxide by the anthraquinone process according to claim 9, characterized in that: the gas phase inlet (22) of the primary hydrogenation tower (1) is arranged on the outer wall of the hydrogenation tower shell corresponding to the space between the two catalyst beds (8).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320782350.2U CN219689338U (en) | 2023-04-08 | 2023-04-08 | Hydrogenation system for producing hydrogen peroxide by anthraquinone process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320782350.2U CN219689338U (en) | 2023-04-08 | 2023-04-08 | Hydrogenation system for producing hydrogen peroxide by anthraquinone process |
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| Publication Number | Publication Date |
|---|---|
| CN219689338U true CN219689338U (en) | 2023-09-15 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202320782350.2U Active CN219689338U (en) | 2023-04-08 | 2023-04-08 | Hydrogenation system for producing hydrogen peroxide by anthraquinone process |
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| CN (1) | CN219689338U (en) |
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