Organic silicon monomer synthesis reactor with heat transfer structure
By adopting a jacketed half-tube and spiral coil structure in the silicone reactor, the uneven temperature distribution and media deflection problems are solved, the conversion rate is improved, and the uniform heat exchange effect of a large-scale design is achieved.
Patent Information
- Application Number
- CN202422259021.7
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-09-14
- Publication Date
- 2025-07-22
- Estimated Expiration
- 2034-09-14
AI Technical Summary
Existing silicone reactors have problems such as uneven temperature distribution, low reaction medium deviation and low conversion rate, especially in large-scale designs, it is difficult to achieve uniform heat exchange and efficient conversion.
The structural design with jacketed half-tube and spiral coil is adopted. The thermally conductive oil is heat-exchanged through the jacketed half-tube and spiral coil. The thermally conductive oil flows from bottom to top, and the reaction medium flows axially in the annular gap between the spiral coil and the shell, achieving unbiased flow and uniform temperature distribution.
The radial and axial temperature distribution in the reactor is achieved, which avoids local overtemperature, improves the conversion rate, and meets the needs of large-scale designs.
Smart Images
Figure CN223128013U_ABST
Abstract
Description
Technical Field
[0001] The utility model belongs to the technical field of silicone reactors, and particularly relates to a silicone monomer synthesis reactor with a heat transfer structure. Background Art
[0002] In a silicone device, a silicone monomer synthesis reactor is the core equipment for silicone production. Inside the reactor, gaseous chloromethane and solid silicon powder react under the action of a copper-based catalyst to produce silicone monomers. The reaction is complex, and its main reaction is: Si + 2CH3Cl → (CH3)2SiCl2. The operating temperature is 280°C to 320°C. This reaction is a strong exothermic reaction, and it is necessary to promptly remove the heat released by the reaction from the reactor to ensure the smooth progress of the reaction.
[0003] At present, there are mainly two forms of heat transfer in silicone reactors: finger tubes and U-shaped tubes. The cooling medium, generally heat-conducting oil, flows inside the tubes. The heat-conducting oil flows inside the tubes and exchanges heat with the medium in the bed layer through the partition wall. The temperature of the heat-conducting oil rises, thereby removing the reaction heat from the reactor.
[0004] A finger tube is a nested heat exchange tube, which has the forms of series finger tubes and single-pass finger tubes. Among them, the temperature difference on the outer surface of the finger tubes with different passes of the series finger tubes is relatively large, resulting in uneven temperature distribution inside the reactor, local overheating, intensified side reactions, and affecting the conversion rate. The single-pass finger tube can achieve single-tube-pass heat exchange, and the temperature distribution is relatively uniform. However, a perforated plate is required to distribute the finger tubes, and axial discharging cannot be achieved. It is necessary to discharge from the side, resulting in uneven flow. In addition, the diameter of the finger tube is generally 89 - 114 mm, and the structure is a double-layer tube. Under the condition of the same heat exchange capacity, the diameter and weight of the reactor are larger than those of a single tube, and it is not easy to be enlarged.
[0005] In the U-shaped tube form, the heat-conducting oil enters from the top of one end of the U-shaped tube, flows through a single U-shaped bend or multiple U-shaped bends, and then flows out from the top of the other end. The U-shaped tube is similar to two finger tubes connected in series. The temperature difference between the first half and the second half is relatively large, resulting in uneven temperature distribution inside the reactor, local overheating, intensified side reactions, and affecting the conversion rate. Summary of the Invention
[0006] The purpose of the utility model is to solve the above technical problems and provide a silicone monomer synthesis reactor with a heat transfer structure, which has uniform temperature distribution, no uneven flow of the reaction medium, and high conversion rate.
[0007] To achieve the above purpose, the utility model provides a silicone monomer synthesis reactor with a heat transfer structure, which includes a shell, a jacket half-tube, and a spiral coil. The jacket half-tube is sleeved on the outer wall of the shell, and the spiral coil is arranged inside the shell. A shell inlet is provided at the bottom of the outer wall of the shell, and a shell outlet is provided at the upper part. The inlet of the spiral coil is communicated with the shell inlet, and the outlet is communicated with the shell outlet.
[0008] Further, the semi-tube opening of the jacketed semi-tube closely adheres to the outer wall of the housing. The free end at the bottom of the jacketed semi-tube is the jacketed semi-tube inlet, and the free end at the top is the jacketed semi-tube outlet.
[0009] Further, a plurality of jacketed semi-tubes are sleeved in the axial direction of the outer wall of the housing.
[0010] Further, a plurality of both the housing inlets and the housing outlets are arranged and are uniformly arranged along the outer peripheral edge of the housing.
[0011] Further, the spiral coiled pipes are arranged in multiple layers, and the multiple layers of spiral coiled pipes are coaxially sleeved.
[0012] Further, the inlet of each layer of the spiral coiled pipes communicates with the housing inlet through an inlet distributor, and the outlet of each layer of the spiral coiled pipes communicates with the housing outlet through an oil collecting tank.
[0013] Further, the pipe diameter of the spiral coiled pipes is 10 - 89 mm.
[0014] Compared with the prior art, the beneficial effects of the present utility model are as follows:
[0015] 1) Uniform temperature distribution: The heat transfer oil enters from the bottom and exits from the top, without a series structure. The temperature distribution in the axial and radial directions of the reactor is uniform, and there is no problem of local overheating.
[0016] 2) No uneven flow of the reaction medium: The medium in the reactor flows upward axially in the annulus between the spiral coiled pipes and flows out from the top outlet, without the problem of uneven flow.
[0017] 3) High conversion rate: The temperature distribution in the reactor bed is uniform, without local overheating, and side reactions are reduced, which is beneficial to improving the conversion rate.
[0018] 4) For a reactor of the same volume, the heat exchange area is large, meeting the design requirements for the enlargement of the device. Description of the Drawings
[0019] Figure 1 It is a schematic diagram of the organosilicon monomer synthesis reactor with a heat removal structure of the present utility model. Detailed Embodiments
[0020] The present utility model will be further described below in conjunction with the drawings and specific embodiments.
[0021] As Figure 1The silicone monomer synthesis reactor with a heat transfer structure shown in the figure includes a shell 5, a jacket half-pipe 6 and a spiral coil 4. The jacket half-pipe 6 is sleeved on the outer wall of the shell 5, and the spiral coil 4 is arranged inside the shell 5. The half-pipe opening of the jacket half-pipe 6 is closely attached to the outer wall of the shell 5. The bottom free end of the jacket half-pipe 6 is the jacket half-pipe inlet 2, and the top free end is the jacket half-pipe outlet 8. Cooling medium, generally heat-conducting oil, flows through the half-pipe. The heat-conducting oil enters the half-pipe from the jacket half-pipe inlet 2, flows upward in the half-pipe, takes away the reaction heat near the shell 5, the temperature rises, and finally flows out from the jacket half-pipe outlet 8. According to the heat exchange requirement, a plurality of jacket half-pipes 6 are sleeved in the axial direction of the outer wall of the shell.
[0022] The bottom of the outer wall of the shell 5 is provided with a shell inlet 1, and the upper part is provided with a shell outlet 9. The inlet of the spiral coil 4 is communicated with the shell inlet 1, and the outlet is communicated with the shell outlet 9. Cooling medium, generally heat-conducting oil, flows through the spiral coil 4. The heat-conducting oil flows into the spiral coil 4 from the shell inlet 1, spirally flows upward in the spiral coil 4, removes the reaction heat inside the reactor, the temperature rises, and finally flows out from the shell outlet 9. According to the heat exchange requirement, a plurality of shell inlets 1 and shell outlets 9 are arranged and are evenly arranged along the outer periphery of the shell. The medium in the reactor reacts in the circular cross-section space of the spiral coil and the annular cross-section space formed between the spiral coil and the shell 5, and flows upward along the axis, and finally flows out from the top outlet of the shell.
[0023] If the diameter of the reactor is large and a large amount of heat is released inside, the spiral coil 4 can be arranged in multiple layers. The multiple layers of spiral coils 4 are coaxially sleeved. The inlet of each layer of spiral coil 4 is communicated with the shell inlet 1 through an inlet distributor 3, and the outlet of each layer of spiral coil 4 is communicated with the shell outlet 9 through an oil collecting tank 7. The heat-conducting oil enters the inlet distributor 3 from the shell inlet 1, then flows into each spiral coil 4, spirally flows upward in each spiral coil 4, removes the reaction heat inside the reactor, the temperature rises, enters the oil collecting tank 7, and finally flows out from the shell outlet 9.
[0024] As Figure 1 described above, including an inner layer spiral coil, a middle layer spiral coil and an outer layer spiral coil. According to actual needs, more layers of spiral coils can be arranged. The medium in the reactor reacts in the circular cross-section space of the inner layer spiral coil and the annular cross-section space between the spiral coil layers, and flows upward along the axis, and finally flows out from the top outlet of the shell.
[0025] Determine the diameter and pitch of the spiral coil according to the height of the reactor, the pressure drop of the heat-conducting oil, and the inlet and outlet temperatures of the heat-conducting oil. The pipe diameter of the spiral coil 4 is 10 - 89 mm, preferably 19 mm.
[0026] Inside the shell, a spiral coil pipe is adopted, and the cooling medium, generally heat-conducting oil, flows through the pipe. An inlet for the heat-conducting oil is arranged at the bottom of the shell, and an outlet for the heat-conducting oil is arranged at the top of the shell. The heat-conducting oil flows upward in a single pipe without a series structure. As the temperature of the heat-conducting oil rises, the reaction heat is removed from the reactor, and the radial temperature distribution in the reactor is uniform. At the same time, the bottom of the shell is a dense phase region where the reaction is intense and a large amount of heat is released. The heat-conducting oil is fed from the bottom and discharged from the top. The low temperature of the inlet oil temperature can quickly remove the reaction heat at the bottom, making the axial temperature distribution in the reactor uniform and preventing local overheating. The medium in the reactor flows upward along the axis in the annulus between the spiral coil pipes and is discharged from the top outlet without the problem of uneven flow. At the same time, the spiral coil pipe can well absorb the axial expansion difference between the spiral coil pipe and the shell, reducing the thermal stress.
Claims
1. An organosilicon monomer synthesis reactor with a heat transfer structure, characterized in that: It includes a housing (5), a jacket half pipe (6) and a spiral coil pipe (4). The jacket half pipe (6) is sleeved on the outer wall of the housing (5), and the spiral coil pipe (4) is arranged inside the housing (5). A housing inlet (1) is provided at the bottom of the outer wall of the housing (5), and a housing outlet (9) is provided at the upper part. The inlet of the spiral coil pipe (4) is communicated with the housing inlet (1), and the outlet is communicated with the housing outlet (9).
2. The organosilicon monomer synthesis reactor with a heat transfer structure according to claim 1, wherein: The half pipe opening of the jacket half pipe (6) is closely attached to the outer wall of the housing (5). The free end at the bottom of the jacket half pipe (6) is the jacket half pipe inlet (2), and the free end at the top is the jacket half pipe outlet (8).
3. The organosilicon monomer synthesis reactor with a heat transfer structure according to claim 1, wherein: A plurality of jacket half pipes (6) are sleeved in the axial direction of the outer wall of the housing (5).
4. The organosilicon monomer synthesis reactor with a heat transfer structure according to claim 1, wherein: A plurality of the housing inlets (1) and a plurality of the housing outlets (9) are both arranged and evenly arranged along the outer periphery of the housing (5).
5. The silicone monomer synthesis reactor with a heat transfer structure according to claim 1, characterized in that: The spiral coil pipe (4) is arranged in multiple layers, and the multiple layers of spiral coil pipes (4) are coaxially sleeved and arranged.
6. The organosilicon monomer synthesis reactor with a heat transfer structure according to claim 5, wherein: The inlet of each layer of the spiral coil pipe (4) is communicated with the housing inlet (1) through an inlet distributor (3), and the outlet of each layer of the spiral coil pipe (4) is communicated with the housing outlet (9) through an oil collecting tank (7).
7. The silicone monomer synthesis reactor with a heat transfer structure according to claim 1, wherein: The pipe diameter of the spiral coil pipe (4) is 10 - 89 mm.