Integrated moving bed reactor
Through the integrated design of mobile bed reactor, the buffer tank and the reactor are connected through a support cylinder, and a catalyst pipeline is installed inside, which solves the problems of pipeline leakage and heat loss and achieves a safe and energy-saving operation effect.
Patent Information
- Application Number
- CN202422484378.5
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-10-14
- Publication Date
- 2025-08-22
- Estimated Expiration
- 2034-10-14
AI Technical Summary
In existing mobile bed reactors, the pipeline connection between the buffer tank and the reactor is prone to leakage and there is a problem of heat loss, and the exposed catalyst conveying pipeline leads to heat loss.
Adopting an integrated design, the buffer tank and the reactor are connected through a support cylinder, and a catalyst pipeline is installed inside the support cylinder. The reactor head cover structure is improved to the support cylinder structure, and the buffer tank and the support cylinder are sealed to avoid exposed catalyst pipelines.
It reduces the heat dissipation loss of the catalyst pipeline, reduces construction difficulty, and reduces safety hazards and operating energy consumption through one-time lifting and maintenance.
Smart Images
Figure CN223249277U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the field of petrochemical industry, in particular to an integrated moving bed reactor. Background Art
[0002] Moving bed reactors are one of the most commonly used reactors in the petrochemical industry. Due to the unique characteristics of the production process, most existing moving bed reactors feature catalyst collection, buffering, preheating, or reduction equipment installed above the moving bed. The buffer tank and reactor are connected by pipes. This structural arrangement makes maintenance difficult and poses the risk of leakage from pipe flanges. Furthermore, the exposed catalyst delivery pipelines pose a risk of heat loss.
[0003] Therefore, it is very necessary to develop a moving bed reactor that can solve the above problems. Utility Model Content
[0004] The purpose of the utility model is to overcome the problem in the prior art that leakage and heat loss are prone to occur when a pipe is used to connect the reactor and the buffer tank, and to provide an integrated moving bed reactor. The moving bed reactor has an integrated design, and a support tube is used to connect the buffer tank and the reactor. The original independent elliptical head of the reactor is improved into a support tube structure. The support tube structure has the functions of sealing the reactor head cover and supporting the buffer tank. A catalyst pipeline is arranged inside the support tube to avoid the catalyst pipeline being exposed, which can reduce the heat dissipation of the catalyst pipeline.
[0005] In order to achieve the above object, the utility model provides a moving bed reactor, which includes a buffer tank 1, a support tube 2 and a reactor body 3;
[0006] The outlet of the buffer tank 1 is connected to the inlet of the support cylinder 2, and the outlet of the support cylinder 2 is connected to the inlet of the reactor body 3;
[0007] Catalyst pipelines 4 are arranged inside the support tube 2 along the inner wall of the support tube, and the number of the catalyst pipelines 4 is 4-20.
[0008] Through the above technical solution, the beneficial effects obtained are as follows:
[0009] (1) The integrated design connects the buffer tank and the reactor body through a support tube, and a catalyst pipeline is arranged inside the support tube to avoid the catalyst pipeline being exposed to the outside and reduce the heat dissipation of the catalyst pipeline;
[0010] (2) Preferably, the connection between the buffer tank and the support tube is sealed. During maintenance, the buffer tank, support tube and catalyst pipeline are hoisted and repaired at one time, which can reduce the construction difficulty and achieve safe and energy-saving operation of the reactor. BRIEF DESCRIPTION OF THE DRAWINGS
[0011] Figure 1 It is a schematic diagram of the moving bed reactor of the present utility model.
[0012] Description of Reference Numerals
[0013] DETAILED DESCRIPTION
[0014] The endpoints of the ranges and any values disclosed herein are not limited to the precise ranges or values, and these ranges or values should be understood to include values close to these ranges or values. For numerical ranges, the endpoints of each range, the endpoints of each range and individual point values, and the individual point values can be combined with each other to obtain one or more new numerical ranges, which should be considered to be specifically disclosed herein.
[0015] In order to make the technical problems, technical solutions and beneficial effects to be solved by the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not intended to limit the present invention.
[0016] It should be noted that when an element is referred to as being “fixed on” or “disposed on” another element, it may be directly on the other element or indirectly on the other element. When an element is referred to as being “connected to” another element, it may be directly connected to the other element or indirectly connected to the other element.
[0017] It should be understood that the terms "length", "width", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", etc., indicating the orientation or position relationship, are based on the orientation or position relationship shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present invention.
[0018] The moving bed reactor provided by the utility model is as follows Figure 1 As shown, the moving bed reactor includes a buffer tank 1, a support cylinder 2 and a reactor body 3;
[0019] The outlet of the buffer tank 1 is connected to the inlet of the support cylinder 2, and the outlet of the support cylinder 2 is connected to the inlet of the reactor body 3;
[0020] Catalyst pipelines 4 are arranged inside the support tube 2 along the inner wall of the support tube, and the number of the catalyst pipelines 4 is 4-20.
[0021] The moving bed reactor provided by the present invention connects the buffer tank 1 and the reactor body 3 with a support tube 2 to obtain an integrated moving bed reactor, improves the original reactor head cover structure, and improves the original independent elliptical head of the reactor into a support tube structure. The support tube structure has the functions of sealing the reactor head cover and supporting the buffer tank. At the same time, a catalyst pipeline 4 is arranged inside the support tube to realize the transportation of catalyst between the buffer tank 1 and the reactor body 3.
[0022] In some preferred embodiments of the present invention, the number of catalyst lines 4 is 4-20. For example, the number may be 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19, or 20, with 6-18 being preferred. The catalyst lines 4 are evenly distributed along the circumference of the central axis of the support tube 2, and the distances between the catalyst lines 4 and the central axis of the support tube 2 are equal. When the number of catalyst lines 4 is an even number, the catalyst lines are symmetrically distributed about the central axis of the support tube.
[0023] In some embodiments of the present invention, the inner diameter of the catalyst pipeline 4 is 40-150 mm, for example, it can be 40 mm, 50 mm, 60 mm, 70 mm, 80 mm, 90 mm, 100 mm, 110 mm, 120 mm, 130 mm, 140 mm, 150 mm, and any value in a range consisting of any two values.
[0024] In the present invention, the length of the catalyst line 4 is not particularly limited, as long as it can transport the catalyst between the buffer tank 1 and the reactor body 3 .
[0025] In the present invention, the catalyst pipeline 4 is used to transport the catalyst required for the reaction. The catalyst pipeline is arranged inside the support tube 2 to avoid the catalyst pipeline being exposed, which can reduce the heat dissipation of the catalyst pipeline by about 5°C.
[0026] In some preferred embodiments of the present invention, the linear distance between the central axes of two adjacent catalyst lines 4 on the lower bottom surface of the support tube 2 is 200-500 mm. Preferably, the catalyst lines 4 are arranged perpendicular to the lower bottom surface of the support tube 2, extending through the lower bottom surface of the support tube 2 into the reactor body 3. This ensures that the catalyst lines 4 are evenly distributed within the support tube 2 according to the aforementioned arrangement, allowing the catalyst to be uniformly discharged from the support tube and into the reactor body 3, thereby preventing excessive catalyst from being introduced into a single catalyst line.
[0027] In the present invention, a pipe connector (not shown) is also provided on the catalyst pipeline 4. The catalyst pipeline 4 is a segmented pipeline, and the pipe connector connects the segments of the catalyst pipeline to facilitate maintenance and prevent leakage of the catalyst pipeline, which could cause fire risks at high temperatures and pose a safety hazard.
[0028] In some preferred embodiments of the present invention, the connection method between the buffer tank 1 and the support tube 2 is not particularly limited, and preferably a sealed connection is adopted. There is no particular limitation on the implementation of the sealed connection, and for example, welding can be used.
[0029] In the present invention, the moving bed reactor is an integrated moving bed reactor. The connection method between the buffer tank 1 and the support tube 2 improves the head cover structure of the existing reactor. The buffer tank 1, support tube 2, catalyst pipeline 4 and reactor body 3 are connected in an integrated design, and the catalyst pipeline 4 is arranged inside the support tube 2. Compared with the traditional connection between the buffer tank and the reactor through a pipeline, the integrated moving bed reactor reduces the heat loss caused by leakage of the catalyst delivery pipeline during the alkane dehydrogenation reaction. At the same time, a one-time maintenance hoisting is adopted during maintenance, which reduces the construction difficulty and saves maintenance and installation time.
[0030] According to some specific embodiments of the present invention, the oblique angle α formed by the side of the support tube 2 and the lower bottom surface is 30-90°. For example, it can be 30°, 35°, 40°, 45°, 50°, 55°, 60°, 65°, 70°, 75°, 80°, 85°, 90°, or any value in a range consisting of any two values, and is preferably 60-80°.
[0031] When the bevel angle α is less than 90°, the support tube 2 is conical; when the bevel angle α is 90°, the support tube 2 is cylindrical. The angle α is controlled to allow the catalyst to quickly pass through the catalyst line 4 and enter the catalyst bed in the reactor body 3 (not shown), avoiding blockage of the catalyst line 4.
[0032] In the present invention, the buffer tank 1 is a conventional buffer tank in the art, which can collect and store the introduced catalyst while keeping the pressure of the entire moving bed reactor basically stable, avoiding pressure fluctuations caused by introducing reaction raw materials into the reactor body 3 and causing safety hazards.
[0033] In some embodiments of the present invention, the inner diameter of the buffer tank 1 is 300-3000 mm. For example, the inner diameter of the buffer tank 1 is 300 mm, 400 mm, 500 mm, 600 mm, 700 mm, 800 mm, 900 mm, 1000 mm, 1200 mm, 1400 mm, 1600 mm, 1800 mm, 2000 mm, 2200 mm, 2400 mm, 2600 mm, 2800 mm, 3000 mm, and any value in the range consisting of any two values, preferably 500-2600 mm.
[0034] In some embodiments of the present invention, the height of the buffer tank 1 is 600-8000 mm, for example, it can be 600 mm, 800 mm, 1000 mm, 1500 mm, 2000 mm, 2500 mm, 3000 mm, 3500 mm, 4000 mm, 4500 mm, 5000 mm, 5500 mm, 6000 mm, 6500 mm, 7000 mm, 7500 mm, 8000 mm, and any value in the range consisting of any two values, preferably 800-6000 mm.
[0035] In some embodiments of the present invention, the height-to-diameter ratio of the buffer tank 1 is 1:0.5-20.
[0036] In the present invention, the reactor body 3 is connected to the support tube 2 via a flange 5. The support tube 2 and the reactor body 3 can be detachably connected in this manner, making it easier to hoist and repair the buffer tank 1 and the support tube 2, thus reducing construction difficulty.
[0037] In some embodiments of the present invention, the height of the support tube 2 is not particularly limited. Preferably, the ratio of the height of the support tube 2 to the height of the buffer tank 1 is 0.5-5:1.
[0038] In some embodiments of the present invention, the type of the reactor body 3 is not particularly limited, as long as it can perform alkane dehydrogenation reaction. The reactor body 3 further includes a catalyst bed and a reaction raw material inlet (not shown in the figure). The catalyst bed is used to load the catalyst, and the reaction raw material inlet is used to introduce the alkane dehydrogenation reaction raw material. The arrangement of the catalyst bed and the reaction raw material inlet is not particularly limited, and those skilled in the art can adjust them adaptively.
[0039] In the present invention, the inner diameter of the reactor body 3 is 300-6000 mm, for example, 300 mm, 400 mm, 500 mm, 600 mm, 700 mm, 800 mm, 900 mm, 1000 mm, 1500 mm, 2000 mm, 2500 mm, 3000 mm, 3500 mm, 4000 mm, 4500 mm, 5000 mm, 5500 mm, 6000 mm, and any value in the range consisting of any two values, preferably 500-5000 mm.
[0040] In the present invention, the height of the reactor body 3 is 600-20000 mm, for example, 600 mm, 700 mm, 800 mm, 900 mm, 1000 mm, 1500 mm, 2000 mm, 2500 mm, 3000 mm, 3500 mm, 4000 mm, 4500 mm, 5000 mm, 5500 mm, 6000 mm, 7000 mm, 8000 mm, 9000 mm, 10000 mm, 12000 mm, 14000 mm, 16000 mm, 18000 mm, 20000 mm, and any value in the range composed of any two values, preferably 800-16000 mm.
[0041] The moving bed reactor provided by the present invention is suitable for alkane dehydrogenation reaction, preferably suitable for propane dehydrogenation reaction. The conditions of the alkane dehydrogenation reaction are not particularly limited, and those skilled in the art can select conventional alkane dehydrogenation reaction conditions.
[0042] According to some preferred embodiments of the present invention, Figure 1 As shown, the catalyst for alkane dehydrogenation enters the buffer tank 1, enters the catalyst bed of the reactor body 3 through the catalyst pipeline 4 set in the support tube 2, and the reaction raw materials are introduced through the reaction raw material inlet of the reactor body 3, and the alkane dehydrogenation reaction is carried out in the reactor body 3.
[0043] In the present invention, those skilled in the art can set a product outlet and a catalyst outlet on the reactor body 3 according to the conditions of the alkane dehydrogenation reaction, which will not be described in detail here.
[0044] The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. Within the technical concept of the present invention, various simple variations of the technical solution of the present invention may be made, including combining the various technical features in any other appropriate manner. These simple variations and combinations should also be considered as disclosed in the present invention and fall within the scope of protection of the present invention.
Claims
1. An integrated moving bed reactor, characterized in that: The moving bed reactor comprises a buffer tank (1), a support cylinder (2) and a reactor body (3); The outlet of the buffer tank (1) is connected to the inlet of the support cylinder (2), and the outlet of the support cylinder (2) is connected to the inlet of the reactor body (3); Catalyst pipelines (4) are arranged inside the support tube (2) along the inner wall of the support tube, and the number of the catalyst pipelines (4) is 4-20.
2. The integrated moving bed reactor according to claim 1, characterized in that: The catalyst pipelines (4) are evenly distributed along the circumference of the central axis of the support cylinder (2), and the distances between the catalyst pipelines (4) and the central axis of the support cylinder (2) are equal.
3. The integrated moving bed reactor according to claim 1, characterized in that: On the bottom surface of the support cylinder (2), the straight-line distance between the central axes of two adjacent catalyst pipelines (4) is 200-500 mm.
4. The integrated moving bed reactor according to claim 1, characterized in that: The inner diameter of the catalyst pipeline (4) is 40-150 mm.
5. The integrated moving bed reactor according to claim 1, characterized in that: The oblique angle α formed between the side of the support tube (2) and the lower bottom surface is 30-90°; When the bevel angle α is less than 90°, the support tube (2) is a cone; when the bevel angle α is 90°, the support tube (2) is a cylinder.
6. The integrated moving bed reactor according to claim 1, characterized in that: The support cylinder (2) is connected to the reactor body (3) via a flange (5).
7. The integrated moving bed reactor according to claim 1, characterized in that: The buffer tank (1) has an inner diameter of 300-3000 mm and a height of 600-8000 mm.
8. The integrated moving bed reactor according to claim 1 or 7, characterized in that: The moving bed reactor is an integrated moving bed reactor.
9. The integrated moving bed reactor according to claim 1, characterized in that: The height-to-diameter ratio of the buffer tank (1) is 1:0.5-20.
10. The integrated moving bed reactor according to claim 1, characterized in that: The inner diameter of the reactor body (3) is 300-6000 mm, and the height is 500-20000 mm.