CN209778300U - Hydrogenation bed layer for producing hydrogen peroxide by anthraquinone method fixed bed - Google Patents
Hydrogenation bed layer for producing hydrogen peroxide by anthraquinone method fixed bed Download PDFInfo
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- CN209778300U CN209778300U CN201920588186.5U CN201920588186U CN209778300U CN 209778300 U CN209778300 U CN 209778300U CN 201920588186 U CN201920588186 U CN 201920588186U CN 209778300 U CN209778300 U CN 209778300U
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Abstract
The utility model discloses a hydrogenation bed layer of anthraquinone method fixed bed production hydrogen peroxide solution includes second inertia porcelain ball layer, catalyst grained layer, changeover portion inertia porcelain ball layer, first inertia porcelain ball layer from bottom to top, and the porcelain ball particle diameter ratio of changeover portion inertia porcelain ball layer and catalyst grained layer is 0.8 ~ 1.5: 1. The ceramic ball particle size of the transition section inert ceramic ball layer is less than 3mm, and the laying height is 100-300 mm. The first inert ceramic ball layer is paved with alumina balls with the grain diameter of 5-8 mm and the height of 100-300 mm. The utility model discloses an add and establish changeover portion inertia porcelain ball layer to this section porcelain ball particle diameter and highly inject, make liquid phase, gaseous phase before getting into the catalyst layer, reached or be close to catalyst layer characteristic distribution state, finally reach the purpose that reduces the anthraquinone and take place excessive hydrogenation reaction volume in catalyst layer part, effectively reduce the anthraquinone loss, reduce the accessory substance production, reduce the subsequent handling load, create considerable economic benefits.
Description
Technical Field
The utility model relates to the technical field of hydrogen peroxide industrial production, in particular to a hydrogenation bed layer for producing hydrogen peroxide by an anthraquinone method fixed bed.
Background
In the actual industrial application of the fixed bed of the anthraquinone method for producing hydrogen peroxide, the gas-liquid distributor of the hydrogenation reactor is unreasonable in design, unqualified in manufacture and installation and the like, so that the poor distribution of materials is caused, namely the initial poor distribution of the materials is caused. The large-scale maldistribution of the materials in the catalyst bed can cause the local irreversible excessive hydrogenation reaction of the catalyst bed, and the continuous loss of the effective component anthraquinone in the working solution. Finally, the defects of high anthraquinone consumption, high consumption of activated alumina of the regenerated working solution, high frequency of replacing the activated alumina and the like are caused. In addition, the generated byproducts are not processed in time and are accumulated along with the running of the system, and the content of the byproducts reaches a certain range, so that the normal production is seriously influenced, and the comprehensive cost of the hydrogen peroxide production is greatly increased.
At present, inert alumina ceramic balls are paved on the upper part and the lower part of each catalyst section in a hydrogenation tower fixed bed for producing hydrogen peroxide by an anthraquinone method, and the general paving method comprises the following steps: laid from bottom to top in sequenceInert alumina balls, a 20-mesh stainless steel wire net,Catalyst particles, a 20-mesh stainless steel wire mesh andInert alumina ceramic balls. The alumina ceramic balls on the catalyst particle layer in the paving method have no good material distribution effect, namely the size and the filling height of the alumina ceramic balls on the catalyst layer are not selected according to the hydraulics characteristic of the catalyst layer, and the alumina ceramic balls are pavedthe alumina ceramic ball of (1).
Therefore, in the existing reactor for producing hydrogen peroxide by the anthraquinone process fixed bed, the material distribution scheme obviously still has inconvenience and defects, and needs to be further improved. How to create a new hydrogenation bed layer for producing hydrogen peroxide by an anthraquinone method fixed bed, so that the materials are distributed by simple and reasonable inert fillers to achieve the state that the materials enter a catalyst bed layer and are well distributed, the consumption of anthraquinone is reduced, and finally the comprehensive production cost of hydrogen peroxide is reduced, which is an urgent need of improvement in the current industry.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is to provide a hydrogenation bed layer of anthraquinone method fixed bed production hydrogen peroxide solution, make it distribute through simple reasonable filler, reach the material and get into the good state of catalyst bed layer distribution, anthraquinone consumption reduces, finally makes hydrogen peroxide solution synthesize manufacturing cost descend to overcome the not enough of the material distribution condition of current anthraquinone method fixed bed production hydrogen peroxide solution.
In order to solve the technical problem, the utility model provides a hydrogenation bed layer of anthraquinone method fixed bed production hydrogen peroxide solution, including the catalyst grained layer, lay the first inert porcelain ball layer in its upper portion and lay the second inert porcelain ball layer in its lower part, it is equipped with changeover portion inert porcelain ball layer to add between catalyst grained layer and the first inert porcelain ball layer, the porcelain ball particle diameter on changeover portion inert porcelain ball layer with the catalyst grained diameter ratio of particle on catalyst grained layer is 0.8 ~ 1.5: 1.
The further improvement is that the ceramic ball of the transition section inert ceramic ball layer is an alumina ceramic ball, and the grain diameter of the alumina ceramic ball is less than 3 mm.
Further improvement, the laying height of the inert ceramic ball layer of the transition section is 100-300 mm.
Further improvement, the first inert ceramic ball layer is paved with alumina balls with the grain size of 5-8 mm, and the paving height is 150-300 mm.
Further improvement, alumina balls with the particle size of 3-10 mm are paved on the second inert ceramic ball layer, and the paving height is 150-300 mm.
further improve, all lay stainless steel net from bottom to top between second inertia porcelain ball layer, catalyst grained layer, changeover portion inertia porcelain ball layer and the first inertia porcelain ball layer of laying in proper order.
Further improvement, the stainless steel wire mesh is a 10-100 mesh wire mesh.
After adopting such design, the utility model discloses following advantage has at least:
1. The utility model discloses an add between catalyst grained layer and first inert porcelain ball layer and establish changeover portion inert porcelain ball layer, and make the porcelain ball particle diameter on changeover portion inert porcelain ball layer be 80% ~ 150% of the catalyst grained diameter of catalyst grained layer, and the porcelain ball particle diameter is less than 3mm, make the material before getting into the catalyst layer, reach or be close its characteristic distribution state in the catalyst grained layer, effectively avoided because of the bad consequence of the material that leads to of initial distribution in catalyst grained layer gas-liquid distribution, finally reach the purpose that reduces anthraquinone in catalyst grained layer local emergence excessive hydrogenation volume, do benefit to the reasonable completion of anthraquinone hydrogenation.
2. And the design of the hydrogenation bed layer is more scientific, reasonable and more characterized by the limitation of the height of the inert ceramic ball layer of the transition section and the limitation of the particle size and the height of the first and second inert ceramic ball layers. The anthraquinone loss in a working solution system can be effectively reduced, the generation of byproducts is reduced, the load of subsequent auxiliary processes is reduced, the comprehensive cost is reduced, and considerable economic benefits are created.
Drawings
The foregoing is only an overview of the technical solutions of the present invention, and in order to make the technical means of the present invention more clear, the present invention will be further described in detail with reference to the accompanying drawings and the detailed description.
FIG. 1 is a schematic structural diagram of a hydrogenation bed layer for producing hydrogen peroxide by an anthraquinone process fixed bed.
Detailed Description
The utility model discloses according to the hydraulics characteristic of anthraquinone method fixed bed production hydrogen peroxide solution hydrogenation bed, to the size of inert porcelain ball on the catalyst grained layer with fill highly carry out the rational distribution, avoided the extensive maldistribution of material to last to have the catalyst layer that reacts catalytic action from inert porcelain ball layer, can reduce the consumption of anthraquinone in the anthraquinone method fixed bed production hydrogen peroxide solution hydrogenation process to a great extent. Specific examples are as follows.
Referring to the attached drawing 1, the hydrogenation bed layer for producing hydrogen peroxide by the anthraquinone method fixed bed in the embodiment includes a first inert ceramic ball layer 2, a catalyst particle layer 1 and a second inert ceramic ball layer 3 which are sequentially laid from top to bottom.
In this embodiment, a transition inert ceramic ball layer 4 is additionally disposed between the catalyst particle layer 1 and the first inert ceramic ball layer 2, the ceramic ball particle size of the transition inert ceramic ball layer 4 is related to the catalyst particle size used by the fixed bed, and for example, the ratio of the ceramic ball particle size of the transition inert ceramic ball layer 4 to the catalyst particle size of the catalyst particle layer 1 is 0.8-1.5: 1.
In a preferred embodiment, the ceramic balls of the transition section inert ceramic ball layer 4 are inert alumina ceramic balls, and the grain size of the ceramic balls is less than 3 mm.
The purpose of setting the inert ceramic ball layer of the transition section is as follows: after the materials pass through the transition section inert ceramic ball layer and before entering the catalyst particle layer, the distribution state of the materials can approach/reach the characteristic distribution state of the materials in the catalyst particle layer, so that the materials reach a good distribution state before entering the catalyst particle layer.
The height calculation formula of the transition section inert ceramic ball layer 4 is as follows (1):
Wherein: c is a distribution point arrangement function on the gas-liquid distributor, and if the distribution point arrangement function is triangular distribution, 0.031 is taken, and if the distribution point arrangement function is quadrilateral distribution, 0.027 is taken; DPD is the density of distribution points on the gas-liquid distributor, 1/m2(ii) a Z is the height m of the inert ceramic ball layer of the transition section; dr is the radial diffusion coefficient of the working fluid in the inert ceramic ball layer of the transition section, and m.
In this embodiment, in the hydrogenation reactor for producing hydrogen peroxide by using the fixed bed of the anthraquinone process, the operating temperature is set to be 45-70 ℃, the operating pressure is set to be 0.15-0.45 MpaG, the distribution points on the gas-liquid distributor 6 at the upper end of the reactor are arranged in a regular triangle, and the distribution points are denseThe degree of the reaction is 50 to 120/m2(ii) a According to the size of catalyst particles, the diameter of a ceramic ball of the inert ceramic ball layer of the transition section is selected to be 2.2-3 mm, the radial diffusion coefficient of working liquid in the inert ceramic ball layer of the transition section is 0.0012-0.003 m, and the height of the inert ceramic ball layer of the transition section is calculated to be within the range of 100-300 mm according to the comprehensive economic requirement and the formula (1).
In the embodiment, the hydrogenation bed layer is formed by paving alumina balls with the particle size of 5-8 mm on the first inert ceramic ball layer 2, and the paving height is 100-300 mm. And selecting the second inert ceramic ball layer 3, paving alumina balls with the grain size of 3-10 mm, and paving the alumina balls with the height of 150-300 mm.
And stainless steel wire meshes 5 are laid between the second inert ceramic ball layer 3, the catalyst particle layer 1, the transition section inert ceramic ball layer 4 and the first inert ceramic ball layer 2 which are laid in sequence from bottom to top. The mesh number of the stainless steel wire mesh 5 is 10-100 meshes.
Aiming at the porcelain ball particle size and height setting in this embodiment, can effectively avoid among the industrial application, because of the adverse consequence that gas-liquid distributor design is unreasonable, the manufacturing installation is not up to standard and causes, excessive hydrogenation when effectively having avoided the working solution to get into the catalyst granular layer has effectively reduced anthraquinone loss and follow-up auxiliary process's load in the working solution system, reduces comprehensive cost, reaches good considerable economic benefits.
According to the description, the filling method of the hydrogenation bed layer for producing hydrogen peroxide by the anthraquinone method fixed bed comprises the following steps: from down up lay second inertia porcelain ball layer 3, stainless steel net 5, catalyst grained layer 1, stainless steel net 5, changeover portion inertia porcelain ball layer 4, stainless steel net 5 and first inertia porcelain ball layer 2 in proper order.
Specifically, alumina balls with the particle size of 3-10 mm are paved on the second inert ceramic ball layer 3, and the paving height is 150-300 mm; laying a 10-100 mesh stainless steel wire net 5 on the steel wire net; then laying catalyst particles of the catalyst particle layer 1, and laying a 10-100 mesh stainless steel wire net 5 on the catalyst particles; then laying a transition section inert ceramic ball layer 4, wherein the ratio of the ceramic ball particle size of the transition section inert ceramic ball layer 4 to the catalyst particle size of the catalyst particle layer 1 is 0.8-1.5: 1, and the filling height of the transition section inert ceramic ball layer 4 is generally 100-300 mm; then laying a 10-100 mesh stainless steel wire net 5 on the steel wire net; then, a first inert ceramic ball layer 2 is laid, alumina balls with the particle size of 5-8 mm are laid on the first inert ceramic ball layer 2, and the laying height is 100-300 mm. In industrial design and construction, a combined scheme of series connection and parallel connection of a plurality of hydrogenation beds can be made according to the requirements of device productivity, required hydrogenation depth, allowable hydrogenation depth and the like.
The utility model discloses the hydrogenation bed layer of anthraquinone method fixed bed production hydrogen peroxide solution is through increasing one section inert filler that is close with catalyst particle size on the catalyst particular layer for the material has reached or is close the characteristic distribution state of catalyst particular layer before getting into the catalyst particular layer, effectively avoids because of initial poor result that leads to the material in catalyst particular layer maldistribution. Finally, the aim of reducing excessive hydrogenation reaction amount of the anthraquinone on the local part of the catalyst layer is achieved, anthraquinone loss in a working solution system is effectively reduced, byproduct generation is reduced, the load of subsequent auxiliary processes is reduced, the comprehensive cost is reduced, and considerable economic benefit is created.
The above description is only for the preferred embodiment of the present invention, and not intended to limit the present invention in any way, and those skilled in the art can make various modifications, equivalent changes and modifications using the above-described technical content, all of which fall within the scope of the present invention.
Claims (7)
1. The hydrogenation bed for producing hydrogen peroxide by the anthraquinone process fixed bed comprises a catalyst particle layer, a first inert ceramic ball layer paved on the catalyst particle layer and a second inert ceramic ball layer paved on the lower portion of the catalyst particle layer, and is characterized in that a transition section inert ceramic ball layer is additionally arranged between the catalyst particle layer and the first inert ceramic ball layer, and the ratio of the ceramic ball particle size of the transition section inert ceramic ball layer to the catalyst particle size of the catalyst particle layer is 0.8-1.5: 1.
2. The hydrogenation bed for producing hydrogen peroxide by an anthraquinone process fixed bed according to claim 1, wherein the ceramic balls of the transition section inert ceramic ball layer are alumina ceramic balls, and the particle size of the alumina ceramic balls is less than 3 mm.
3. The hydrogenation bed layer for producing hydrogen peroxide by using the anthraquinone method fixed bed according to claim 2, wherein the laying height of the transition section inert ceramic ball layer is 100-300 mm.
4. The hydrogenation bed layer for producing hydrogen peroxide through the anthraquinone method fixed bed according to claim 3, wherein alumina balls with the particle size of 5-8 mm are laid on the first inert ceramic ball layer, and the laying height is 100-300 mm.
5. The hydrogenation bed layer for producing hydrogen peroxide through the anthraquinone method fixed bed according to claim 4, wherein alumina balls with the particle size of 3-10 mm are laid on the second inert ceramic ball layer, and the laying height is 150-300 mm.
6. The hydrogenation bed layer for producing hydrogen peroxide by an anthraquinone process fixed bed according to any one of claims 1 to 5, wherein stainless steel wire meshes are laid among the second inert ceramic ball layer, the catalyst particle layer, the transition section inert ceramic ball layer and the first inert ceramic ball layer which are laid in sequence from bottom to top.
7. the hydrogenation bed layer for producing hydrogen peroxide by using the anthraquinone method fixed bed according to claim 6, wherein the stainless steel wire mesh is a wire mesh with 10-100 meshes.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201920588186.5U CN209778300U (en) | 2019-04-26 | 2019-04-26 | Hydrogenation bed layer for producing hydrogen peroxide by anthraquinone method fixed bed |
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| CN201920588186.5U CN209778300U (en) | 2019-04-26 | 2019-04-26 | Hydrogenation bed layer for producing hydrogen peroxide by anthraquinone method fixed bed |
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