CN210065169U - Hydrogenation tower for preparing hydrogen peroxide - Google Patents
Hydrogenation tower for preparing hydrogen peroxide Download PDFInfo
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- CN210065169U CN210065169U CN201920473294.8U CN201920473294U CN210065169U CN 210065169 U CN210065169 U CN 210065169U CN 201920473294 U CN201920473294 U CN 201920473294U CN 210065169 U CN210065169 U CN 210065169U
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Abstract
The utility model discloses a hydrogenation tower for hydrogen peroxide preparation, which comprises a shell, wherein a catalyst reaction section arranged above and a gas-liquid separation section which is arranged below the catalyst reaction section and communicated with the catalyst reaction section are arranged in the shell, a liquid distributor arranged above the catalyst reaction section is arranged at the top in the shell, and a liquid inlet pipe arranged outside the shell is communicated with the liquid distributor through a connecting pipe; the catalyst reaction section comprises at least two catalyst reaction layers which are arranged in series, the adjacent two catalyst reaction layers are separated by a grid plate, and a gas-liquid distribution disc is arranged above each catalyst reaction layer; compared with the prior art, the utility model, through the design and the arrangement of each structure, make the raw materials get into the even distribution in back in the casing, and improved the reaction time of material, reduce the loss of material to reach the purpose that improves production efficiency, reduction loss, reduction in production cost.
Description
Technical Field
The utility model relates to a preparation technical field of hydrogen peroxide solution, concretely relates to hydrogenation tower for hydrogen peroxide solution preparation.
Background
At present, the method for producing hydrogen peroxide by an anthraquinone method in domestic industry comprises a suspension kettle nickel catalyst process, a fixed bed palladium catalyst process, a fluidized bed process and the like, wherein the fixed bed palladium catalyst process of the anthraquinone method is the mainstream of the domestic hydrogen peroxide production process due to the advantages of low investment, high yield, simple operation, low usage amount of used palladium catalyst, high activity, easy regeneration, safe use and the like, and the production capacity accounts for more than 95 percent of the total capacity.
The anthraquinone process of producing hydrogen peroxide with 2-alkyl anthraquinone as hydrogen carrier includes hydrogenation reaction and oxidation reaction in arene and trioctyl phosphate solvent under the catalysis of palladium catalyst.
In the industrial production of the hydrogen peroxide by the prior anthraquinone method, the gas-liquid distribution of the hydrogenation tower is uneven and the conversion efficiency is low, so that the catalyst efficiency is low, the consumption of raw materials such as anthraquinone and the like is increased, the production cost is increased, and the market competitiveness is reduced.
SUMMERY OF THE UTILITY MODEL
To the not enough that exists among the prior art, the utility model aims to provide a hydrogenation tower for hydrogen peroxide solution preparation to solve prior art, hydrogenation tower gas-liquid distribution is inhomogeneous and conversion efficiency is low, leads to raw materials consumption such as catalyst efficiency low, anthraquinone to increase, has increased manufacturing cost, has reduced market competition's problem.
In order to achieve the above purpose, the utility model adopts the following technical scheme: the hydrogenation tower for preparing hydrogen peroxide comprises a shell, wherein a catalyst reaction section arranged above and a gas-liquid separation section which is arranged below the catalyst reaction section and communicated with the catalyst reaction section are arranged in the shell, a liquid distributor arranged above the catalyst reaction section is arranged at the top in the shell, and the liquid distributor is communicated with a liquid inlet pipe arranged outside the shell through a connecting pipe;
the catalyst reaction section comprises at least two catalyst reaction layers which are arranged in series, the adjacent two catalyst reaction layers are separated by a grid plate, and a gas-liquid distribution disc is arranged above each catalyst reaction layer.
Compared with the prior art, the utility model discloses following beneficial effect has:
the hydrogenation tower is divided into a catalyst reaction section and a gas-liquid separation section, raw materials enter a shell from a liquid inlet pipe, enter the catalyst reaction section after being uniformly distributed through a liquid distributor, react through at least two catalyst reaction layers arranged in series, the reaction time is prolonged, the reaction efficiency is improved, and meanwhile, reaction materials entering the catalyst reaction layers from one catalyst reaction layer are further uniformly distributed through a gas-liquid distribution plate, so that the reaction efficiency is further improved; finally, gas-liquid separation is carried out on the reacted materials through a gas-liquid separation section, so that the materials can be recovered for secondary reaction, and the loss of the materials is reduced; so as to achieve the purposes of improving the production efficiency, reducing the loss and reducing the production cost.
Drawings
Fig. 1 is a schematic structural view of the present invention;
fig. 2 is a partially enlarged view of fig. 1.
Detailed Description
The present invention will be described in further detail with reference to the following embodiments:
reference numerals in the drawings of the specification include: the device comprises a shell 1, a liquid distributor 2, a liquid inlet pipe 3, a grid plate 4, a gas-liquid distribution plate 5, a distribution base plate 51, a distribution pipe 52, a distribution block 53, a connecting pipe 6, a vertical pipe 61, a horizontal pipe 62, a fixing plate 7, a gas-liquid separator 8, a palladium coal-touching layer 9 and a manhole 10.
Examples
Referring to fig. 1 and 2: the hydrogenation tower for preparing hydrogen peroxide comprises a shell 1, wherein a catalyst reaction section arranged above and a gas-liquid separation section which is arranged below the catalyst reaction section and communicated with the catalyst reaction section are arranged in the shell 1, a liquid distributor 2 arranged above the catalyst reaction section is arranged at the top in the shell 1, and a liquid inlet pipe 3 arranged outside the shell 1 is communicated on the liquid distributor 2 through a connecting pipe 6; the catalyst reaction section includes two at least catalyst reaction layers that establish ties and set up, separates through grid tray 4 between two adjacent catalyst reaction layers, and every catalyst reaction layer top all is provided with gas-liquid distribution dish 5, and catalyst reaction layer has two in this embodiment.
In order to ensure that the raw materials enter the shell 1 to be uniformly distributed so as to improve the reaction efficiency; the liquid distributor 2 comprises a liquid distribution disc, a plurality of spray heads are uniformly distributed on the liquid distribution disc, and raw materials introduced into the liquid inlet pipe 3 are introduced into the liquid distribution disc through the connecting pipe 6 and then are uniformly distributed to the top of the shell 1 through the spray heads on the liquid distribution disc; the gas-liquid distribution discs 5 comprise distribution base plates 51, a plurality of distribution pipes 52 are arranged on the upper surfaces of the distribution base plates 51, and the side wall of the upper end of each distribution pipe 52 is connected with a distribution block 53 arranged above the distribution pipe 52 through a connecting block; each structure through in the gas-liquid distribution dish 5 makes it can carry out even distribution to the material of reaction to the even distribution of material reacts in the catalyst reaction layer, improves reaction efficiency.
The adopted connecting pipe 6 comprises a vertical pipe 61 communicated with the liquid distribution disc and a horizontal pipe 62 communicated between the vertical pipe 61 and the liquid inlet pipe 3, and the horizontal pipe 62 is connected with the inner wall of the shell 1 through a fixing plate 7; the space in the shell 1 is reasonably utilized, and the connecting pipe 6 is firmly fixed.
The adopted gas-liquid separation section comprises a gas-liquid separator 8 arranged at the bottom of the tower, and the bottom of the tower is provided with a discharge port; the gas-liquid separator 8 at the bottom of the tower is used for carrying out gas-liquid separation on the reacted materials, the separated liquid is subjected to oxidation reaction in the oxidation tower, the separated gas passes through the return pipe, is mixed with the raw materials in the liquid inlet pipe 3 and then passes through the shell 1 again for secondary reaction, and the loss of the raw materials is reduced; in order to improve the reaction efficiency of the catalyst reaction layer, the catalyst reaction layer comprises a plurality of palladium-contacted coal layers 9 with different thicknesses, two adjacent palladium-contacted coal layers 9 are separated by a separation net, and the stacking modes of the palladium-contacted coal layers 9 in the two adjacent palladium-contacted coal layers are different, so that the flow path of materials is increased, the reaction time of the materials is prolonged, and the reaction efficiency is improved.
A plurality of manholes 10 are arranged on the outer wall of the shell 1 along the axial direction, the manholes 10 are distributed on the outer wall of the shell 1 of the catalytic reaction layer and the side wall of the top of the shell 1, and each catalytic reaction layer is provided with a temperature monitor and a pressure detection meter; through the design of the manhole 10, workers can conveniently enter the shell 1 to replace the palladium catalyst in each catalyst reaction layer and overhaul and maintain the condition in the shell 1; the reaction temperature and pressure of each catalyst reaction layer in the shell 1 are concerned at any moment through a temperature monitor and a pressure detection table so as to adjust the reaction conditions thereof and enable the reaction to have the best reaction efficiency.
Finally, although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that the present invention can be modified or replaced by other means without departing from the spirit and scope of the present invention, which should be construed as limited only by the appended claims.
Claims (7)
1. The hydrogenation tower for preparing hydrogen peroxide is characterized by comprising a shell, wherein a catalyst reaction section arranged above and a gas-liquid separation section which is arranged below the catalyst reaction section and communicated with the catalyst reaction section are arranged in the shell;
the catalyst reaction section comprises at least two catalyst reaction layers which are arranged in series, the adjacent two catalyst reaction layers are separated by a grid plate, and a gas-liquid distribution disc is arranged above each catalyst reaction layer.
2. The hydrogenation tower for hydrogen peroxide preparation according to claim 1, characterized in that: the gas-liquid distribution plate comprises distribution base plates, a plurality of distribution pipes are arranged on the upper surfaces of the distribution base plates, and the side wall of the upper end of each distribution pipe is connected with a distribution block arranged above the distribution pipe through a connecting block.
3. The hydrogenation tower for hydrogen peroxide preparation according to claim 1 or 2, wherein: the liquid distributor comprises a liquid distribution disc, and a plurality of spray heads are uniformly distributed on the liquid distribution disc.
4. The hydrogenation tower for hydrogen peroxide preparation according to claim 3, characterized in that: the connecting pipe comprises a vertical pipe communicated with the liquid distribution disc and a transverse pipe communicated between the vertical pipe and the liquid inlet pipe, and the transverse pipe is connected with the inner wall of the shell through a fixing plate.
5. The hydrogenation tower for hydrogen peroxide preparation according to claim 1, characterized in that: the gas-liquid separation section comprises a gas-liquid separator arranged at the bottom of the tower, and a discharge hole is formed in the bottom of the tower.
6. The hydrogenation tower for hydrogen peroxide preparation according to claim 1, characterized in that: the catalyst reaction layer comprises a plurality of palladium-contacted coal layers with different thicknesses, and every two adjacent palladium-contacted coal layers are separated through a separation net.
7. The hydrogenation tower for hydrogen peroxide preparation according to claim 1, characterized in that: the casing outer wall is provided with a plurality of manholes along the axial direction, the manholes are distributed on the casing outer wall of the catalytic reaction layer and the side wall of the top of the casing, and each catalytic reaction layer is provided with a temperature monitor and a pressure detection meter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920473294.8U CN210065169U (en) | 2019-04-09 | 2019-04-09 | Hydrogenation tower for preparing hydrogen peroxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920473294.8U CN210065169U (en) | 2019-04-09 | 2019-04-09 | Hydrogenation tower for preparing hydrogen peroxide |
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| Publication Number | Publication Date |
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| CN210065169U true CN210065169U (en) | 2020-02-14 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201920473294.8U Active CN210065169U (en) | 2019-04-09 | 2019-04-09 | Hydrogenation tower for preparing hydrogen peroxide |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111977615A (en) * | 2020-07-13 | 2020-11-24 | 中国空分工程有限公司 | Efficient hydrogen peroxide solution production hydrogenation system |
| CN112499594A (en) * | 2020-12-02 | 2021-03-16 | 安徽金禾实业股份有限公司 | Production method of hydrogen peroxide by anthraquinone process |
-
2019
- 2019-04-09 CN CN201920473294.8U patent/CN210065169U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111977615A (en) * | 2020-07-13 | 2020-11-24 | 中国空分工程有限公司 | Efficient hydrogen peroxide solution production hydrogenation system |
| CN112499594A (en) * | 2020-12-02 | 2021-03-16 | 安徽金禾实业股份有限公司 | Production method of hydrogen peroxide by anthraquinone process |
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