Hydroisomerization reaction device
By filling different properties of different properties in multiple catalytic bed layers of hydrogen reaction device, controlling acid and cracking activity, the problem of excessive cracking caused by the super temperature and bias of the catalyst bed layer has achieved a more stable response and higher reaction and higher Product revenue.
Patent Information
- Application Number
- CN202421191808.8
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-05-29
- Publication Date
- 2025-01-28
- Estimated Expiration
- 2034-05-29
AI Technical Summary
In the hydroisomerization reaction, the increase in the temperature of the catalyst bed leads to the exposure of the acidic center, activates cracking activity, and forms a vicious cycle, resulting in uneven reactions and reduced product yields.
Design a hydrogen -derived reaction device. By filling different acidic, compared with the surface area and Kong Rong non -precious metal hydrogen heterogenetic catalyst in multiple catalyst beds to ensure that the acidity of the latter catalyst bed layer is lower than the previous bed layer , Thereby controlling cracking activity at a lower level.
Effectively solve the problem of excessive cracking caused by the super temperature and flow of catalyst beds, maintain the stability and reaction uniformity of the catalyst, and improve the revenue and reaction selectivity of the target product.
Smart Images
Figure CN222401428U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the technical field of petrochemical industry, in particular to a hydrogenation isomerization reaction device. Background Art
[0002] For non-precious metal isomerization catalysts, the hydroisomerization reaction is the process of converting normal alkanes into corresponding branched isoalkanes under hydrogenation conditions through the action of bifunctional catalysts. Such catalysts are bifunctional catalysts composed of molecular sieve carriers and active metals, which have both metal components with hydrogenation-dehydrogenation activity and molecular sieve components with acidic cracking activity. In the hydroisomerization reaction, the hydrogenation-dehydrogenation reaction is carried out on the metal active center, and the isomerization reaction is carried out on the acid center. The balance between the hydrogenation-dehydrogenation activity of the metal component and the acidity of the molecular sieve is crucial, which determines the reaction process of normal alkane isomerization and affects the activity, stability, selectivity and product distribution of the catalyst.
[0003] In the process of hydrogenation isomerization, ammonia injection is generally used to cover part of the acidic centers on the molecular sieve with NH3 to inhibit its cracking activity. However, during the entire reaction process, as the temperature of the catalyst bed increases, the amount of ammonia adsorbed will gradually decrease, the acidic centers will gradually be exposed, and the cracking activity will be activated. The cracking process releases a large amount of heat, which will cause the catalyst bed temperature to continue to rise, forming a vicious cycle. The usual way to deal with this situation is to set up multiple beds and inject cold hydrogen between each bed to lower the reaction temperature. However, for reactors with relatively large diameters, the method of reducing the reaction temperature by injecting cold hydrogen alone may cause the catalyst bed to deflect, resulting in a large radial temperature difference in the catalyst bed. Once the radial temperature difference is formed, there will be uneven reaction, heat accumulation, temperature rise and other phenomena. The amount of ammonia adsorption in the high-temperature zone will decrease, and the catalyst cracking activity will eventually be activated, forming a vicious cycle. Utility Model Content
[0004] In order to overcome the shortcomings and deficiencies in the prior art, the utility model aims to provide a hydroisomerization reaction device.
[0005] The purpose of the utility model is achieved through the following technical scheme: a hydroisomerization reaction device, comprising one or more reactor shells, a plurality of catalyst beds are arranged in the one or more reactor shells, each catalyst bed is filled with at least a portion of hydroisomerization catalyst, and along the direction of medium flow, the acidity of the hydroisomerization catalyst filled in the latter catalyst bed is lower than the acidity of the hydroisomerization catalyst filled in the former catalyst bed.
[0006] Furthermore, the number of the reactor shell is one, and two or more catalyst beds are arranged in the reactor shell.
[0007] Furthermore, three catalyst beds are arranged in the reactor shell.
[0008] Furthermore, the number of the reactor shells is two or more, and at least one catalyst bed is disposed in each reactor shell.
[0009] Furthermore, the number of the reactor shells is three, and a catalyst bed is arranged in each reactor shell.
[0010] Furthermore, along the direction of medium flow, the specific surface area of the hydroisomerization catalyst loaded in the latter catalyst bed is lower than the specific surface area of the hydroisomerization catalyst loaded in the former catalyst bed.
[0011] Furthermore, along the direction of medium flow, the pore volume of the hydroisomerization catalyst loaded in the latter catalyst bed is lower than the pore volume of the hydroisomerization catalyst loaded in the former catalyst bed.
[0012] Furthermore, the hydroisomerization catalyst is a non-precious metal hydroisomerization catalyst.
[0013] The beneficial effect of the utility model is that the hydroisomerization reaction device of the utility model can solve the problems of excessive cracking caused by bed overheating, bed deviation, etc. in the hydroisomerization process by controlling the acidity of the non-precious metal hydroisomerization catalyst loaded in the latter catalyst bed to be lower than the acidity of the non-precious metal hydroisomerization catalyst loaded in the former catalyst bed, so that the cracking activity is always maintained at a low level, and a more stable target product yield can be obtained.
[0014] The hydroisomerization reaction device of the utility model is loaded with isomerization decondensation catalysts of different properties in different beds according to the reaction history of the oil product in the hydroisomerization reaction process, so that the entire reaction process is always under the most ideal reaction conditions, which is beneficial to improving the hydroisomerization selectivity and reducing the hydrocracking selectivity. BRIEF DESCRIPTION OF THE DRAWINGS
[0015] Figure 1 It is a structural schematic diagram of the first embodiment of the utility model.
[0016] Figure 2 It is a structural schematic diagram of the second embodiment of the present utility model.
[0017] The reference numerals are: reactor shell 1 , material inlet 11 , product outlet 12 , catalyst bed 2 , first catalyst bed 21 , second catalyst bed 22 , third catalyst bed 23 . DETAILED DESCRIPTION
[0018] In order to facilitate the understanding of those skilled in the art, the following embodiments and attached Figure 1-2 To further illustrate the present invention, the contents mentioned in the implementation modes are not intended to limit the present invention.
[0019] like Figure 1 The figure shows a first embodiment of a hydroisomerization reaction device, comprising a reactor shell 1, in which a plurality of catalyst beds 2 are arranged, each catalyst bed 2 is loaded with at least a portion of a hydroisomerization catalyst, and along the direction of medium flow, the acidity of the hydroisomerization catalyst loaded in the latter catalyst bed 2 is lower than the acidity of the hydroisomerization catalyst loaded in the former catalyst bed 2.
[0020] In this embodiment, three catalyst beds 2 are arranged in the reactor shell 1. A material inlet 11 is arranged at the top of the reactor shell 1, and a product outlet 12 is arranged at the bottom of the reactor shell 1. In the reactor shell 1, the flow direction of the material is from top to bottom. The three catalyst beds 2 include a first catalyst bed 21, a second catalyst bed 22 and a third catalyst bed 23 arranged in sequence from top to bottom. The catalyst loaded in the first catalyst bed 21 has higher acidity, specific surface area and pore volume than the catalyst loaded in the second catalyst bed 22. The catalyst in the second catalyst bed 22 has higher acidity, specific surface area and pore volume than the catalyst loaded in the third catalyst bed 23. And so on. As needed, a cold hydrogen injection point can be set between each catalyst bed 2. In other embodiments, the number of the catalyst beds 2 can also be two or more than three. Any obvious replacement without departing from the concept of the utility model is within the protection scope of the utility model.
[0021] In this embodiment, along the direction of medium flow, the specific surface area of the hydroisomerization catalyst loaded in the latter catalyst bed 2 is lower than the specific surface area of the hydroisomerization catalyst loaded in the former catalyst bed 2 .
[0022] In this embodiment, along the direction of medium flow, the pore volume of the hydroisomerization catalyst loaded in the latter catalyst bed 2 is lower than the pore volume of the hydroisomerization catalyst loaded in the former catalyst bed 2 .
[0023] In this embodiment, the hydroisomerization catalyst is a non-precious metal hydroisomerization catalyst.
[0024] During the implementation process, the temperature of the raw material entering the first catalyst bed 21 is about 340°C, and the temperature of the raw material exiting the first catalyst bed 21 is about 345°C. At this temperature, the raw material enters the second catalyst bed 22, and the temperature of the raw material exiting the second catalyst bed 22 is about 350°C. Then, the raw material enters the third catalyst bed 23 at this temperature, and the temperature of the raw material exiting the third catalyst bed 23 is about 355°C. During the hydrogenation process, ammonia is generally required to be injected into the catalyst bed 2 to inhibit the cracking activity of the catalyst. As the reaction proceeds, the isomerization rate gradually increases, and the required isomerization temperature also gradually increases. However, at the same time, a higher temperature will desorb ammonia on the catalyst surface, exposing more acidic centers, activating cracking activity, resulting in an increase in cracking rate and a reduction in the yield of the target product. After the catalyst is loaded using the hydrogenation isomerization reaction device of the utility model, as the reaction proceeds, the acidity of the catalyst gradually decreases, the specific surface area gradually decreases, and the pore volume gradually decreases, so that the cracking activity is always maintained at a low level, and a more stable yield of the target product can be obtained.
[0025] like Figure 2 The figure shows a second embodiment of a hydroisomerization reaction device, which includes two or more reactor shells 1, each reactor shell 1 is provided with at least one catalyst bed 2, each catalyst bed 2 is loaded with at least a portion of hydroisomerization catalyst, and along the direction of medium flow, the acidity of the hydroisomerization catalyst loaded in the latter catalyst bed 2 is lower than the acidity of the hydroisomerization catalyst loaded in the former catalyst bed 2.
[0026] In this embodiment, the number of the reactor shells 1 is three, and each reactor shell 1 is provided with a catalyst bed 2. A material inlet 11 is provided at the top of the first reactor shell 1, and a product outlet 12 is provided at the bottom of the last reactor shell 1. In the reactor shell 1, the flow direction of the material is from top to bottom, and each reactor shell 1 is connected by a pipeline. The three reactor shells are respectively provided with a first catalyst bed 21, a second catalyst bed 22 and a third catalyst bed 23. The catalyst loaded in the first catalyst bed 21 has higher acidity, specific surface area and pore volume than the catalyst loaded in the second catalyst bed 22, and the catalyst loaded in the second catalyst bed 22 has higher acidity, specific surface area and pore volume than the catalyst loaded in the third catalyst bed 23, and so on. Cold hydrogen injection points can be provided between each reactor shell 1 as needed. In other embodiments, the number of the reactor shells 1 can also be two or more than three, and each reactor shell 1 can be provided with more than one catalyst bed 2. Any obvious replacement without departing from the concept of the utility model is within the protection scope of the utility model.
[0027] The other parts of this embodiment are the same as those of the first embodiment and will not be described again.
[0028] The above embodiments are preferred implementation schemes of the present invention. In addition, the present invention can also be implemented in other ways. Any obvious replacement without departing from the concept of the present invention is within the protection scope of the present invention.
Claims
1. A hydroisomerization reaction device, comprising one or more reactor shells, characterized in that: A plurality of catalyst beds are arranged in one or more reactor shells, each catalyst bed is loaded with at least a portion of hydroisomerization catalyst, and along the direction of medium flow, the acidity of the hydroisomerization catalyst loaded in the latter catalyst bed is lower than the acidity of the hydroisomerization catalyst loaded in the former catalyst bed.
2. A hydroisomerization reaction device according to claim 1, characterized in that: The number of catalysts in the reactor shell is one, and two or more catalyst beds are arranged in the reactor shell.
3. A hydroisomerization reaction device according to claim 2, characterized in that: Three catalyst beds are arranged in the reactor shell.
4. A hydroisomerization reaction device according to claim 1, characterized in that: The number of the reactor shells is two or more, and at least one catalyst bed is arranged in each reactor shell.
5. A hydroisomerization reaction device according to claim 4, characterized in that: The number of the reactor shells is three, and a catalyst bed is arranged in each reactor shell.
6. A hydroisomerization reaction device according to claim 1, characterized in that: Along the direction of medium flow, the specific surface area of the hydroisomerization catalyst loaded in the latter catalyst bed is lower than the specific surface area of the hydroisomerization catalyst loaded in the former catalyst bed.
7. A hydroisomerization reaction device according to claim 1, characterized in that: Along the direction of medium flow, the pore volume of the hydroisomerization catalyst loaded in the latter catalyst bed is lower than the pore volume of the hydroisomerization catalyst loaded in the former catalyst bed.
8. A hydroisomerization reaction device according to claim 1, characterized in that: The hydroisomerization catalyst is a non-precious metal hydroisomerization catalyst.