Efficient hydrogenation tower
By using the helical catalyst frame assembly layer in the hydrogenation tower, the problems of reaction in unevenness and large equipment volume in traditional hydrogenation towers are solved, and more efficient hydrogenation reactions and lower anthraquinone consumption are achieved, which improves the equipment utilization and operating cycle.
Patent Information
- Application Number
- CN202421762353.0
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-07-24
- Publication Date
- 2025-07-25
- Estimated Expiration
- 2034-07-24
AI Technical Summary
The traditional hydrogenation tower structure causes uneven reaction between the working liquid and hydrogen, and there are phenomena such as deflection flow, groove flow, wall flow, etc. The local reaction overheating produces a large number of anthraquinone degradants, the catalyst utilization rate is low, the equipment volume is large, and the investment is high.
The helical catalyst frame assembly layer is adopted, including the Johnson grid layer, the catalyst distribution frame, the catalyst protectant layer and the gas-liquid distributor layer, to improve the catalyst protectant layer to be uniform spiral distribution, prevent bias and blockage, and improve reaction uniformity and efficiency.
The stable uniformity of the hydrogenation reaction is achieved, the anthraquinone consumption is reduced, the equipment volume and investment is reduced, the catalyst utilization is improved, and the operation cycle is extended.
Smart Images
Figure CN223144678U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to a hydrogenation tower, in particular to an efficient hydrogenation tower, belonging to the technical field of chemical equipment. Background Technique
[0002] Most domestic hydrogen peroxide (hydrogen peroxide) production adopts the anthraquinone process. In the production of hydrogen peroxide by the anthraquinone process, as a catalyst component for hydrogen peroxide production, the palladium catalyst reacts with hydrogen in a hydrogenation tower with a working solution composed of 2-ethyl anthraquinone, heavy aromatic hydrocarbons, trioctyl phosphate, and tetrabutylurea to produce a hydrogenated solution containing hydroanthraquinone and tetrahydroanthraquinone. The hydrogenated solution enters the oxidation process for reaction to produce hydrogen peroxide.
[0003] As the main reaction equipment for the hydrogen peroxide production device, the working solution hydrogenation equipment is a key equipment in hydrogen peroxide production. The structure of this equipment has a great relationship with the hydrogenation speed, the uniformity of hydrogenation, and the generation amount of degradation products.
[0004] The internal structure of the original traditional process hydrogenation tower is a key factor in the performance indicators of the hydrogen peroxide device. The filling method of the catalyst in the hydrogenation tower of the hydrogen peroxide device always adopts the method of grids and porcelain balls. This method greatly limits the filling amount of the palladium catalyst, thus affecting the hydrogenation effect. Such a filling method has the following disadvantages: 1. In the process of the working solution and hydrogen flowing downward and reacting in the catalyst layer, phenomena such as uneven flow, channel flow, and wall flow will occur; 2. The hydrogenation reaction in each part of the catalyst layer is uneven, and local reaction overheating occurs in some places, and a large amount of anthraquinone degradation products are generated in the overheated reaction places; 3. Due to the appearance of a large amount of degradation products, the consumption of anthraquinone increases significantly, affecting the physical properties of the working solution. The working solution has a high viscosity and poor coagulation effect, manifested as the thickening of the working solution layer under the tray in the extraction tower or the phenomenon of water in the raffinate; 4. The utilization rate of the catalyst in this filling method is too low, and it is difficult to improve the production efficiency (hydrogenation efficiency). The traditional process hydrogenation tower requires a large amount of catalyst, and the equipment volume needs to be made larger. Content of the Utility Model
[0005] Based on the above background, the purpose of the present utility model is to provide an efficient hydrogenation tower that overcomes the deficiencies of the prior art and occupies a small area, and solves the problems described in the background technique.
[0006] In order to achieve the above utility model purpose, the present utility model provides the following technical solutions:
[0007] An efficient hydrogenation tower includes a catalyst section tower body and a gas-liquid separation section tower body. The catalyst section tower body is located above the gas-liquid separation section tower body, and the catalyst section tower body is communicated with the gas-liquid separation section tower body;
[0008] Inside the catalyst section tower body, several layers of spiral catalyst frame assemblies are provided. The spiral catalyst frame assembly layer includes a Johnson mesh layer, a catalyst distribution frame, a catalyst protective agent layer, and a gas-liquid distributor layer. The Johnson mesh layer, the catalyst distribution frame, the catalyst protective agent layer, and the gas-liquid distributor layer are arranged in sequence from bottom to top, and the Johnson mesh layer, the catalyst distribution frame, the catalyst protective agent layer, and the gas-liquid distributor layer are all connected to the catalyst section tower body.
[0009] Preferably, a hydrogen inlet is provided at the top of the catalyst section tower body, and the hydrogen inlet is communicated with the catalyst section tower body.
[0010] Preferably, a working liquid inlet is provided at the top of the catalyst section tower body, and the working liquid inlet is communicated with the catalyst section tower body.
[0011] Preferably, a hydrogenated tail gas outlet is provided at the upper part of the gas-liquid separation section tower body, and a hydrogenated liquid outlet is provided at the lower part of the gas-liquid separation section tower body. The hydrogenated tail gas outlet and the hydrogenated liquid outlet are both communicated with the gas-liquid separation section tower body.
[0012] Preferably, the number of the spiral catalyst frame assembly layers is at least three.
[0013] Preferably, a catalyst protective agent is arranged inside the catalyst protective agent layer, and the catalyst protective agent is detachably and fixedly connected to the catalyst protective agent layer.
[0014] Preferably, the hydrogen inlet is arranged vertically.
[0015] Preferably, the working liquid inlet is arranged vertically.
[0016] Hydrogen and the working liquid enter the catalyst section tower body through the hydrogen inlet and the working liquid inlet. When gas-liquid distribution is carried out first, the working liquid flows from the support mesh plate of the gas-liquid distributor layer to the spray plate of the gas-liquid distributor and sprays downward. Hydrogen enters downward through the downcomer on the distribution plate of the gas-liquid distributor and enters together with the uniformly distributed working liquid into the catalyst protective agent layer to fully react. In this process, the hydrogenation reaction is more stable and uniform than the traditional process, and the local degradation side reaction is greatly reduced; the consumption of anthraquinone in the system is greatly reduced, and the anthraquinone consumption is only 50% of that of the traditional process.
[0017] In the traditional process before improvement, the catalyst protective agent layer was a porcelain ball layer and a wire mesh. The erosion of a large amount of working liquid caused the porcelain balls to roll and wear and easily powder; the dust mixed with the working liquid easily blocked the pores of the palladium catalyst, resulting in a decrease in catalyst activity and a shortening of the operation cycle.
[0018] The improved catalyst protection frame has a uniform spiral distribution, which divides the catalyst carrier into several small channels, forming an anti-deviation flow assembly to prevent phenomena such as deviation flow, channel flow, and wall flow during the hydrogenation process of the working liquid catalyst layer; it solves the problem of a large amount of anthraquinone degradation products generated by local reaction overheating.
[0019] The Johnson grid layer can make the distribution of the union liquid uniform, and it has good circulation performance, is not easy to be blocked, and improves the renewal speed of the working liquid on the catalyst surface. The hydrogenation reaction ability and the spraying density are increased by 5%.
[0020] The spiral catalyst frame assembly layer is provided with three or more layers, which can combine the hydrogenation part of the catalyst section tower body with the gas-liquid separation part of the gas-liquid separation section tower body, reducing the equipment investment and the floor area. Compared with the traditional hydrogenation equipment, the overall volume is smaller, the equipment investment is more economical, and at the same time the reaction ability is increased. The catalyst utilization rate is higher and the catalyst consumption is less compared with the traditional hydrogenation equipment. The catalyst consumption is only 60% of the traditional process amount.
[0021] Compared with the prior art, the utility model has the following advantages:
[0022] 1. The hydrogenation reaction is more stable and uniform than the traditional process, and the local degradation side reaction is greatly reduced; the consumption of anthraquinone in the system is greatly reduced, and the anthraquinone consumption is only 70% of the traditional process;
[0023] 2. Prevent phenomena such as uneven flow, channel flow, and wall flow during the hydrogenation of the working liquid catalyst layer; solve the problem of a large amount of anthraquinone degradation products generated by local reaction overheating;
[0024] 3. Solve the problem that the porcelain balls are prone to powdering and blocking the catalyst pores, resulting in a decrease in reaction and a shortening of the operation cycle;
[0025] 4. The Johnson grid layer replaces the grille, with uniform distribution, good circulation performance, not easy to be blocked, and improves the catalyst performance; the hydrogenation reaction ability and the spraying density are increased by 5%;
[0026] 5. The overall volume becomes smaller and the reaction ability is increased; the catalyst utilization rate is higher and the catalyst consumption is less compared with the traditional hydrogenation equipment. The catalyst consumption is only 60% of the traditional process amount. BRIEF DESCRIPTION OF THE DRAWINGS
[0027] In order to more clearly illustrate the technical solutions in the embodiments of the present utility model or the prior art, the following will briefly introduce the drawings required for the description of the embodiments or the prior art. Obviously, the drawings in the following description are only the embodiments of the present utility model. For those of ordinary skill in the art, other drawings can be obtained according to the provided drawings without creative efforts.
[0028] Figure 1 It is a schematic diagram of the overall structure of the high-efficiency hydrogenation tower of the present utility model.
[0029] In the figure: 1. Catalyst section tower body; 2. Gas-liquid separation section tower body; 3. Spiral catalyst frame component layer; 301. Johnson grid layer; 302. Catalyst distribution frame; 303. Catalyst protective agent layer; 304. Gas-liquid distributor layer; 4. Hydrogen inlet; 5. Working fluid inlet; 6. Hydrogenation tail gas outlet; 7. Hydrogenated liquid outlet. Specific embodiments
[0030] The technical solution of the present invention will be further specifically described below through specific embodiments and in conjunction with the accompanying drawings. It should be understood that the implementation of the present invention is not limited to the following embodiments, and any formal modification and / or change made to the present invention will fall within the protection scope of the present invention.
[0031] In the present invention, unless otherwise specified, all parts and percentages are in weight units, and the equipment and raw materials used can be purchased from the market or are commonly used in the art. The methods in the following embodiments are conventional methods in the art unless otherwise specified. The components or equipment in the following embodiments are general standard parts or components known to those skilled in the art unless otherwise specified, and their structures and principles can all be known by those skilled in the art through technical manuals or through conventional experimental methods.
[0032] The following makes a detailed description of the embodiments of the present invention in conjunction with the accompanying drawings. In the following detailed description, for the convenience of explanation, many specific details are elaborated to provide a comprehensive understanding of the embodiments of the present invention. However, one or more embodiments can also be implemented by those skilled in the art without these specific details.
[0033] As Figure 1 shown, a high-efficiency hydrogenation tower includes a catalyst section tower body 1 and a gas-liquid separation section tower body 2. The catalyst section tower body 1 is located above the gas-liquid separation section tower body 2, and the catalyst section tower body 1 and the gas-liquid separation section tower body 2 are connected.
[0034] The top of the catalyst section tower body 1 is provided with a hydrogen inlet 4 and a working fluid inlet 5. The hydrogen inlet 4 and the working fluid inlet 5 are vertically arranged, and both the hydrogen inlet 4 and the working fluid inlet 5 are connected to the catalyst section tower body 1.
[0035] Inside the catalyst section tower body 1, several layers of spiral catalyst frame assemblies 3 are arranged, and the number of layers of the spiral catalyst frame assemblies 3 is at least three. The spiral catalyst frame assembly layer 3 includes a Johnson grid layer 301, a catalyst distribution frame 302, a catalyst protective agent layer 303, and a gas-liquid distributor layer 304. The Johnson grid layer 301, the catalyst distribution frame 302, the catalyst protective agent layer 303, and the gas-liquid distributor layer 304 are arranged in sequence from bottom to top, and the Johnson grid layer 301, the catalyst distribution frame 302, the catalyst protective agent layer 303, and the gas-liquid distributor layer 304 are all connected to the catalyst section tower body 1. A catalyst protective agent is arranged inside the catalyst protective agent layer 303, and the catalyst protective agent is detachably and fixedly connected to the catalyst protective agent layer 303.
[0036] At the upper part of the gas-liquid separation section tower body 2, a hydrogenation tail gas outlet 6 is arranged, and at the lower part of the gas-liquid separation section tower body 2, a hydrogenated liquid outlet 7 is arranged. The hydrogenation tail gas outlet 6 and the hydrogenated liquid outlet 7 are both communicated with the gas-liquid separation section tower body 2.
[0037] Hydrogen and the working fluid enter the catalyst section tower body 1 through the hydrogen inlet 4 and the working fluid inlet 5. When gas-liquid distribution is carried out first, the working fluid flows from the support mesh plate of the gas-liquid distributor layer 304 to the spray plate of the gas-liquid distributor and sprays downward. Hydrogen enters downward through the downcomer on the distribution plate of the gas-liquid distributor and enters together with the evenly distributed working fluid into the catalyst protective agent layer 303 to fully react. In this process, the hydrogenation reaction is more stable and uniform than the traditional process, and the local degradation side reaction is greatly reduced. As a result, the consumption of anthraquinone in the system is greatly reduced, and the anthraquinone consumption is only 50% of the traditional process.
[0038] Before improvement, the traditional process of the catalyst protective agent layer 303 was a porcelain ball layer and a wire mesh. The erosion of a large amount of working fluid caused the porcelain balls to roll and wear and easily shed powder. The dust mixed with the working fluid easily blocked the pores of the palladium catalyst, resulting in a decrease in catalyst activity and a shortening of the operation cycle.
[0039] The improved catalyst protection frame has its uniform spiral distribution separating the catalyst carrier into several small channels, forming an anti-deviation flow assembly to prevent phenomena such as deviation flow, channel flow, and wall flow during the hydrogenation process of the working fluid catalyst layer. It solves the problem of a large amount of anthraquinone degradation products generated by local reaction overheating.
[0040] The Johnson grid layer 301 can make the distribution of the working fluid uniform, and it has good flow performance and is not easy to be blocked, improving the renewal speed of the working fluid on the catalyst surface. The hydrogenation reaction ability and the spraying density are increased by 5%.
[0041] The spiral catalyst frame component layer 3 is provided with three or more layers, which can combine the hydrogenation part of the catalyst section tower body 1 and the gas-liquid separation part of the gas-liquid separation section tower body 2, reducing equipment investment and floor area. Compared with traditional hydrogenation equipment, the overall volume is smaller, the equipment investment is more economical, and the reaction capacity is increased. The catalyst utilization rate is higher and the amount of catalyst used is less compared with traditional hydrogenation equipment. The amount of catalyst used is only 60% of that in the traditional process.
[0042] The implementation principle of an efficient hydrogenation tower of the present utility model is as follows:
[0043] The working fluid enters the catalyst section tower body 1 from the working fluid inlet 5. Among them, the working fluid is prepared from four chemical raw materials, namely heavy aromatic hydrocarbon, tetrabutylurea, trioctyl phosphate, and 2-ethylanthraquinone, in a certain proportion.
[0044] Hydrogen enters the catalyst section tower body 1 from the hydrogen inlet 4 and is evenly distributed through the gas-liquid distributor layer 304. The working fluid and the hydrogen gas flow downward under a certain reaction pressure and temperature.
[0045] The catalyst protective agent layer 303 contains a catalyst protective agent, which can increase the contact specific surface area by multi-channel stacking, increase the contact with the palladium catalyst, and at the same time solve the problem of generating more alumina dust due to the scouring and collision of porcelain balls during the reaction.
[0046] During the flowing process, under the action of the palladium catalyst, hydrogen reacts with some 2-ethylanthraquinone and tetrahydro-2-ethylanthraquinone in the working fluid to generate hydroanthraquinone. After passing through the multi-layer catalyst distribution frame 302 for reaction, the working fluid becomes a hydrogenated liquid at this time.
[0047] The hydrogenated liquid and the unreacted hydrogen and other gases enter the gas-liquid separation section tower body 2 at the lower part of the catalyst section tower body 1. The unreacted gas and the hydrogenated liquid are separated in the gas-liquid separation section. The tail gas is discharged from the hydrogenation tail gas outlet 6, and the hydrogenated liquid is discharged from the hydrogenated liquid outlet 7.
[0048] Specific examples are used in this article to elaborate on the principle and implementation mode of the present utility model. The description of the above embodiments is only used to help understand the method and its core idea of the present utility model. It should be noted that for those of ordinary skill in the art in this technical field, without departing from the principle of the present utility model, several improvements and modifications can be made to the present utility model, and these improvements and modifications also fall within the protection scope of the claims of the present utility model.
Claims
1. An efficient hydrogenation tower, characterized in that: The efficient hydrogenation tower includes a catalyst section tower body (1) and a gas-liquid separation section tower body (2). The catalyst section tower body (1) is located above the gas-liquid separation section tower body (2), and the catalyst section tower body (1) is communicated with the gas-liquid separation section tower body (2). A number of spiral catalyst frame assembly layers (3) are arranged inside the catalyst section tower body (1). The spiral catalyst frame assembly layer (3) includes a Johnson grid layer (301), a catalyst distribution frame (302), a catalyst protective agent layer (303), and a gas-liquid distributor layer (304). The Johnson grid layer (301), the catalyst distribution frame (302), the catalyst protective agent layer (303), and the gas-liquid distributor layer (304) are arranged in sequence from bottom to top, and the Johnson grid layer (301), the catalyst distribution frame (302), the catalyst protective agent layer (303), and the gas-liquid distributor layer (304) are all connected to the catalyst section tower body (1).
2. The high-efficiency hydrogenation tower according to claim 1, characterized in that: A hydrogen inlet (4) is arranged at the top of the catalyst section tower body (1), and the hydrogen inlet (4) is communicated with the catalyst section tower body (1).
3. The high-efficiency hydrogenation tower according to claim 1, characterized in that: A working liquid inlet (5) is arranged at the top of the catalyst section tower body (1), and the working liquid inlet (5) is communicated with the catalyst section tower body (1).
4. The high-efficiency hydrogenation tower according to claim 1, wherein: A hydrogenation tail gas outlet (6) is arranged at the upper part of the gas-liquid separation section tower body (2), and a hydrogenated liquid outlet (7) is arranged at the lower part of the gas-liquid separation section tower body (2). The hydrogenation tail gas outlet (6) and the hydrogenated liquid outlet (7) are both communicated with the gas-liquid separation section tower body (2).
5. The high-efficiency hydrogenation tower according to claim 1, characterized in that: The number of the spiral catalyst frame assembly layers (3) is at least three layers.
6. The high-efficiency hydrogenation tower according to claim 1, wherein: A catalyst protective agent is arranged inside the catalyst protective agent layer (303), and the catalyst protective agent is detachably and fixedly connected to the catalyst protective agent layer (303).
7. The high-efficiency hydrogenation tower according to claim 2, wherein: The hydrogen inlet (4) is arranged vertically.
8. The high-efficiency hydrogenation tower according to claim 3, wherein: The working liquid inlet (5) is arranged vertically.