Continuous tubular reactor
By introducing a spherical cavity, a mixed fluid structure and a spoiler into a tubular reactor, turbulent mixing is enhanced, the problem of low mass transfer efficiency is solved, continuous production with rapid reaction is achieved, and the selectivity and yield of isopropanolamine are improved.
Patent Information
- Application Number
- CN202422092326.3
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-08-28
- Publication Date
- 2025-09-05
- Estimated Expiration
- 2034-08-28
AI Technical Summary
Existing tubular reactors have low mass transfer efficiency, slow reaction rate, difficult to control heat and mass transfer, and are prone to temperature or concentration gradients, which affect the stability and selectivity of the reaction.
A continuous tubular reactor is designed, which includes a feeding section, a mixing section and a discharging section. A spherical cavity and a mixed fluid are set in the mixing section. A gap is left between the mixed fluid and the inner wall of the spherical cavity, and multiple spoilers are provided to enhance turbulent mixing and prolong the residence time.
It improves the material mixing effect, reduces the occurrence of side reactions, realizes continuous reaction, improves production efficiency, and reduces the operating errors caused by intermittent production.
Smart Images
Figure CN223299994U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the technical field of tubular reactors, in particular to a continuous tubular reactor. The mixer can be used for organic synthesis reactions under high temperature and high pressure conditions, in particular for the reaction of preparing isopropanolamine. Background Art
[0002] Tubular reactors are primarily used for continuous gas-phase, liquid-phase, and gas-liquid-phase reactions. They are simple in structure and easy to manufacture. They feature small volume, large specific surface area, and large heat transfer area per unit volume, making them suitable for reactions with significant thermal effects.
[0003] However, compared to other reactors, tubular reactors have low mass transfer efficiency and slow reaction rates. Furthermore, heat and mass transfer are difficult to control, easily leading to temperature or concentration gradients that compromise reaction stability and selectivity. Therefore, there is a need in the art for a tubular inductor that can enhance mixing, mass transfer, and heat transfer to address these issues. Utility Model Content
[0004] In view of this, the present invention aims to propose a continuous tubular reactor to solve the problems of uneven mixing of reaction materials and low mass transfer and heat transfer efficiency in existing reactors.
[0005] In order to achieve the above-mentioned purpose, the technical solution created by the utility model is implemented as follows:
[0006] A continuous tubular reactor comprises a feeding section, a mixing section, a discharging section and a fluid mixing body. At least one mixing section is provided after the feeding section of the reactor. The inner cavity of the mixing section is one or more spherical cavities connected end to end. At least a portion of the fluid mixing body is provided in one of the spherical cavities. The fluid mixing body is spherical, and a gap is left between the fluid mixing body and the inner wall of the spherical cavity for the reaction material to flow.
[0007] Furthermore, the curvature of the top of the mixing body is smaller than the curvature of the bottom of the mixing body.
[0008] Furthermore, the continuous tubular reactor further comprises a fixed component, which is disposed in the spherical cavity, and the mixed fluid is connected to the spherical cavity via the fixed component.
[0009] Furthermore, the fixing assembly includes a fixing rod and a bracket, the mixing fluid is fixed on the fixing rod, the fixing rod is fixed on the bracket, and the bracket is fixed to the inner wall of the mixing section.
[0010] Furthermore, a distance d1 between the top of the fluid mixture and the top of the spherical cavity is 1 / 8 to 1 / 4 of the radius of the spherical cavity.
[0011] Furthermore, a distance d2 between the inner wall of the spherical cavity and the widest part of the mixed fluid is 1 / 6-1 / 4 of the diameter of the spherical cavity.
[0012] Furthermore, the minimum horizontal distance d3 between the bottom of the inner wall of the spherical cavity and the mixed fluid is 1 / 16-1 / 6 of the diameter of the spherical cavity.
[0013] The continuous tubular reactor also includes a plurality of spoilers, which are arranged on the outer wall of the mixed fluid and are arranged at an angle to the main flow direction of the reaction materials in the reactor; along the main flow direction of the reaction materials, the spoilers are arranged at the widest part of the cross section of the mixed fluid.
[0014] It also includes a plurality of spoilers, wherein the plurality of spoilers are inclined in the same direction or in different directions;
[0015] The plurality of spoilers are arranged on the outer wall of the mixing body at the same height, or on the outer walls of the mixing body at different heights.
[0016] The angle between the spoiler and the main flow direction of the material in the reactor is 30-60 degrees.
[0017] Compared with the prior art, the continuous tubular reactor described in the present invention has the following advantages:
[0018] Compared to the prior art approach of using a narrow, long mixing tube, the continuous tubular reactor provided by this invention incorporates a unique mixing structure, enhancing turbulent mixing within the tube and extending residence time. Because the reaction is rapid, the structure described herein reduces the mixing time of materials after entering the tubular reactor, thereby reducing the occurrence of side reactions. This tubular reactor provides a continuous reaction, improving production efficiency and reducing the additional operations and human errors associated with intermittent production. BRIEF DESCRIPTION OF THE DRAWINGS
[0019] The accompanying drawings, which constitute part of the present invention, are intended to provide a further understanding of the present invention. The exemplary embodiments of the present invention and their descriptions are intended to explain the present invention and do not constitute an improper limitation of the present invention. In the accompanying drawings:
[0020] Figure 1 This is a schematic diagram of the overall structure of a continuous tubular reactor according to the present invention;
[0021] Figure 2 This is a perspective structural diagram of a mixing tube of a continuous tubular reactor according to the present invention;
[0022] Figure 3This is a perspective structural diagram of a mixing tube of a continuous tubular reactor according to the present invention;
[0023] Figure 4 This is a schematic structural diagram of a heat exchange unit of a continuous tubular reactor described in the present invention.
[0024] Description of reference numerals:
[0025] 1-feeding section; 2-feeding port; 3-mixing section; 31-fixing rod; 311-bracket; 32-mixing fluid; 33-spoiler; 8-discharging section; 9-heating structure. DETAILED DESCRIPTION
[0026] The following is a clear and complete description of the technical solutions in the embodiments of the present invention. Obviously, the embodiments described are only part of the embodiments of the present invention, not all of them. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making any creative efforts are within the scope of protection of the present invention.
[0027] It should be noted that, in the absence of conflict, the embodiments of the present invention and the features in the embodiments can be combined with each other.
[0028] The present invention will be described in detail below with reference to the accompanying drawings and in combination with embodiments.
[0029] This embodiment provides a continuous tubular reactor, which includes a feeding section 1 at the top and a discharging section 8 at the bottom. At least one mixing section 3 is provided after the feeding section 1. The specific number of the mixing sections 3 can be set according to actual conditions. The inner cavity of the mixing section 3 is one or more spherical cavities connected end to end. A mixed fluid 32 is provided in the spherical cavity. The mixed fluid 32 is spherical, and at least a part of the mixed fluid 32 is provided in a spherical cavity. More specifically, the mixed fluid 32 can be completely provided in a spherical cavity, or it can be provided in a spherical cavity. Figure 3 and Figure 4 As shown, a portion of its bottom is disposed in the next adjacent spherical cavity, and a gap is left between the mixed fluid 32 and the inner wall of the spherical cavity for the reaction materials to flow.
[0030] Compared to the prior art solution of providing a narrow and long mixing tube, the continuous tubular reactor provided in this embodiment can enhance turbulent mixing and extend residence time within the tube by introducing a unique mixing structure. Because the reaction is rapid, the introduction of the structure described in this application can reduce the mixing time of the materials after entering the tubular reactor and reduce the occurrence of side reactions. This tubular reactor can provide a continuous reaction, improve production efficiency, and reduce the additional operations and human errors caused by intermittent production.
[0031] Specifically, in this embodiment, the continuous tubular reactor further includes a fixing assembly disposed within the spherical cavity, through which the mixing fluid 32 is connected to the spherical cavity. For example, this embodiment provides a specific structure of the fixing assembly, which includes a fixing rod 31 and a bracket 311. The mixing fluid 32 is fixed to the fixing rod 31, which is fixed to the bracket 311. The bracket 311 is fixed to the inner wall of the mixing section 3. The shape of the bracket 311 can be selected as needed.
[0032] Of course, in other embodiments, the position of the mixing body 32 can be fixed by other means. For example, the mixing body 32 can be directly fixedly connected to the mixing body 32 via a plurality of support rods fixed to the inner wall of the spherical cavity, so that the mixing body 32 is suspended within the spherical cavity. Alternatively, the fixing rods 31 or the support rods used to position the mixing body 32 can be configured as telescopic rods to adjust the position of the mixing body 32 within the spherical cavity.
[0033] As a preferred embodiment, the curvature of the top of the mixing body 32 is smaller than that of the bottom of the mixing body 32, resulting in a flatter top. This design aims to increase the lateral velocity of the material after it contacts the mixing body 32, allowing the material to collide with the inner wall of the spherical cavity again and disperse under the blocking effect of the top surface of the mixing body 32, thereby improving the mixing effect of the material.
[0034] Furthermore, in this embodiment, the widest point of the structure of the mixing body 32 is used as the boundary, the upper half of the boundary is ellipsoidal, and the lower half of the boundary is a conical structure. During use, the straight-line distance between the inner wall of the spherical cavity and the outer wall of the mixing body 32 gradually decreases with the direction of fluid flow, and the fluid flow rate gradually increases.
[0035] In the continuous tubular reactor provided in this embodiment, the distances between the fluid mixing body 32 and the spherical inner cavity of the mixing section 3 can be set as needed. Specifically, the diameter of the spherical cavity is larger than the diameter of the feed section 1. For example, the diameter of the spherical cavity can be 1.5 times the diameter of the feed section 1. Sufficient space should be reserved between the top of the fluid mixing body 32 and the top of the spherical inner cavity of the mixing section 3 as a material mixing place; a sufficiently wide gap should also be reserved between the widest part of the fluid mixing body 32 and the spherical inner cavity to reserve enough space for the turbulent materials formed by the spoiler 33; the bottom of the inner wall of the spherical cavity and the horizontal plane of the fluid mixing body 32 (the horizontal plane is defined as Figure 2 and Figure 3 The minimum straight-line distance is determined by the required material flow rate.
[0036] As a preferred embodiment, in the continuous tubular reactor provided in this embodiment, the distance d1 between the top of the mixing fluid 32 and the top of the spherical cavity is 1 / 8-1 / 4 of the radius of the spherical cavity; the distance d2 between the inner wall of the spherical cavity and the widest part of the mixing fluid 32 is 1 / 6-1 / 4 of the diameter of the spherical cavity; and the minimum horizontal distance d3 between the bottom of the inner wall of the spherical cavity and the mixing fluid 32 is 1 / 16-1 / 6 of the diameter of the spherical cavity.
[0037] For example, using a reactor configured in an isopropanolamine system as an example, as a preferred embodiment, the distance d1 between the top of the mixing fluid 32 and the top of the spherical inner cavity of the mixing section 3 is 1 / 4 of the radius of the spherical cavity. The distance d2 between the inner wall of the spherical cavity and the widest point of the mixing fluid 32 is 1 / 6 of the diameter of the spherical cavity. The minimum horizontal distance d3 between the bottom of the inner wall of the spherical cavity and the mixing fluid 32 is 1 / 16 of the diameter of the spherical cavity.
[0038] The continuous tubular reactor provided in this embodiment further includes a plurality of spoilers 33, which are arranged on the outer wall of the fluid mixture 32 and are arranged at an angle to the main flow direction of the reaction materials in the reactor. The length of the spoilers 33 can be set as needed. As a preferred embodiment, the spoilers 33 are arranged at the widest part of the cross section of the fluid mixture 32 along the main flow direction of the reaction materials. To further improve the mixing effect of the materials, in this embodiment, the plurality of spoilers 33 can be tilted in different directions. In other embodiments, the plurality of spoilers 33 can also be arranged on the outer wall of the fluid mixture 32 at different heights. Of course, in other embodiments, other arrangements can also be made as needed.
[0039] As a preferred embodiment, in the continuous tubular reactor provided in the present embodiment, the angle between the spoiler 33 and the main flow direction of the material of the reactor is 30-60 degrees. Exemplary, taking the reactor arranged in the isopropanolamine system as an example, as a preferred embodiment, 8 spoilers 33 can be set at the same height of the mixed fluid 32, and the angle between the spoiler 33 and the length direction of the reactor is 45 degrees.
[0040] In the continuous tubular reactor provided in this embodiment, the feed section 1 can be provided with multiple feed ports 2 for inputting a variety of materials.
[0041] The continuous tubular reactor provided in this embodiment also includes a temperature sensor for measuring temperature, a flow rate sensor for measuring fluid flow rate, a concentration sensor for measuring fluid concentration, and a pressure sensor for measuring pressure in the tubular reaction unit to monitor multiple parameters within the reactor. Specifically, temperature sensors may be installed at the end of the feed section and at the front and middle of the mixing section; flow rate sensors may be installed at the feed section and the discharge section; concentration sensors may be installed at the middle of the mixing section and the discharge section; and pressure sensors may be installed at the feed section, mixing section, and the discharge section.
[0042] The continuous tubular reactor provided in this embodiment also includes a heating structure 9 for heating the feed section 1. This heating structure 9 is wrapped around the outer periphery of the feed section 1 and is used to control the inlet temperature of the reaction materials to a predetermined temperature. Temperature control can also be achieved by wrapping the feed section with insulation material. Of course, in other embodiments, a cooling structure can also be provided as needed.
[0043] The utility model takes the preparation of isopropanolamine by the propylene oxide method and the tubular reactor as an example to introduce the designed tubular reactor. Specific embodiment 1:
[0045] The reaction was conducted using 71.65 wt% propylene oxide and liquid ammonia. The molar ratio of ammonia to propylene oxide in the reactant feed was 5:1. The number of mixing sections 3 was one, and the number of fluid mixtures 32 within the mixing section 3 was two. After the reaction mixture passed through the tubular reactor, the propylene oxide conversion reached 99.9%, with the yields of 1-isopropanolamine, 73.7%, 2-isopropanolamine, 18.2%, and 3-isopropanolamine, 8.1%. Specific embodiment 2:
[0047] The reaction was conducted using 71.65 wt% propylene oxide and liquid ammonia. The molar ratio of ammonia to propylene oxide in the reactant feed was 5:1. There were two mixing sections 3, with four and two mixing fluids 32 in each mixing section, respectively. After the reaction mixture passed through the tubular reactor, the propylene oxide conversion reached 99.9%, with yields of 1-isopropanolamine (69.8%), 2-isopropanolamine (19.4%), and 3-isopropanolamine (10.8%).
[0048] Comparative Example 1:
[0049] 71.65 wt% propylene oxide was reacted with liquid ammonia. The molar ratio of ammonia to propylene oxide in the reactant feed was 5:1. The reaction mass was fed directly into the tubular reactor through feed port 2. The tubular reactor did not contain a mixing section 3. After passing through the tubular reactor, the propylene oxide conversion rate reached 99%, with a yield of 1-isopropanolamine of 34.3%, a yield of 2-isopropanolamine of 28.6%, and a yield of 3-isopropanolamine of 37.1%.
[0050] Currently, isopropanolamine is primarily produced through three methods: the propylene oxide method, the calcium cyanamide method, and the supercritical fluid method. The propylene oxide method is the most widely used. This method involves reacting propylene oxide with aqueous ammonia under a certain pressure and temperature. Currently, the propylene oxide method for producing isopropanolamine in my country faces several challenges, including complex procedures, batch production, difficulty separating products, and low selectivity.
[0051] The continuous tubular reactor provided in this embodiment can provide a better material mixing effect based on the setting mode, and obtain better monoisopropanolamine selectivity and yield.
[0052] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit it. Although the present invention has been described in detail with reference to the above embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the above embodiments, or make equivalent replacements for some or all of the technical features therein. These modifications or replacements do not deviate the essence of the corresponding technical solutions from the scope of the technical solutions of the embodiments of the present invention, and they should all be included in the scope of the claims and description of the present invention.
[0053] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principles of the present invention should be included in the scope of protection of the present invention.
Claims
1. A continuous tubular reactor, characterized in that The reactor comprises a feed section (1), a mixing section (3), a discharge section (8) and a fluid mixing body (32). At least one mixing section (3) is provided after the feed section (1) of the reactor. The inner cavity of the mixing section (3) is one or more spherical cavities connected end to end. At least a portion of the fluid mixing body (32) is provided in one of the spherical cavities. The fluid mixing body (32) is spherical. A gap is left between the fluid mixing body (32) and the inner wall of the spherical cavity for the reaction material to flow.
2. The continuous tubular reactor according to claim 1, characterized in that: The curvature of the top of the mixing body (32) is smaller than the curvature of the bottom of the mixing body (32).
3. The continuous tubular reactor according to claim 1, wherein: It also includes a fixing component, which is arranged in the spherical cavity, and the mixed fluid (32) is connected to the spherical cavity through the fixing component.
4. The continuous tubular reactor according to claim 3, characterized in that: The fixing assembly comprises a fixing rod (31) and a bracket (311), the mixing body (32) is fixed on the fixing rod (31), the fixing rod (31) is fixed on the bracket (311), and the bracket (311) is fixed on the inner wall of the mixing section (3).
5. The continuous tubular reactor according to claim 1, characterized in that: The distance d1 between the top of the mixing body (32) and the top of the spherical cavity is 1 / 8-1 / 4 of the radius of the spherical cavity.
6. The continuous tubular reactor according to claim 1, characterized in that: The distance d2 between the inner wall of the spherical cavity and the widest part of the mixed body (32) is 1 / 6-1 / 4 of the diameter of the spherical cavity.
7. The continuous tubular reactor according to claim 1, characterized in that: The minimum horizontal distance d3 between the bottom of the inner wall of the spherical cavity and the mixed fluid (32) is 1 / 16-1 / 6 of the diameter of the spherical cavity.
8. The continuous tubular reactor according to claim 1, characterized in that: The invention also includes a plurality of spoilers (33), which are arranged on the outer wall of the mixed body (32) and are arranged at an angle with the main flow direction of the reaction material in the reactor; along the main flow direction of the reaction material, the spoilers (33) are arranged at the widest part of the cross section of the mixed body (32).
9. The continuous tubular reactor according to claim 1, characterized in that: It also includes a plurality of spoilers (33), wherein the plurality of spoilers (33) are inclined in the same direction or in different directions; The plurality of spoilers (33) are arranged on the outer wall of the mixing body (32) at the same height, or on the outer walls of the mixing body (32) at different heights.
10. The continuous tubular reactor according to claim 8, characterized in that: The angle between the spoiler (33) and the main flow direction of the material in the reactor is 30-60 degrees.