Methanol synthesis reactor
By employing a spiral tube assembly and a cooling liquid system in the methanol synthesis reactor, the problems of equipment damage and low efficiency in the Lurgi methanol reactor were solved, achieving efficient methanol production and extending catalyst life.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2025-04-03
- Publication Date
- 2026-03-24
AI Technical Summary
The existing Lurgi methanol reactor is a fixed tube sheet heat exchanger with straight reaction tubes. When the temperature rises to the maximum, the reaction force is difficult to eliminate, which can easily damage the equipment. The reaction space is small, resulting in low methanol production efficiency.
The design employs a spiral tube assembly, in which the catalyst flows within the spiral tube, and the coolant passes through the reaction chamber. A gas passage gap is formed between the spiral tube assembly and the catalyst. Catalyst blocking components prevent the catalyst from falling out, and the coolant maintains the temperature. The spiral tube structure increases the reaction space and path, and reduces thermal stress.
It improves methanol production efficiency, extends catalyst life, reduces equipment damage, enhances the ability to withstand high pressure, simplifies the structure, and reduces costs.
Smart Images
Figure CN224024990U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The present application relates to the technical field of methanol synthesis, in particular to a methanol synthesis reactor. BACKGROUND
[0002] The heat exchanger is a device for heat exchange between two or more fluids at different temperatures, which can transfer heat from the fluid at a higher temperature to the fluid at a lower temperature, so that the fluid temperature reaches the process specified index. It is widely used in petroleum, chemical, power, refrigeration and other industrial fields.
[0003] In the related art, methanol is prepared by using a Lurgi methanol reactor. The Lurgi methanol reactor is a fixed tube plate heat exchanger, and the reaction tube is a straight tube. When the temperature rises to the highest temperature, the reaction force is difficult to eliminate, which easily causes damage to the equipment, affects the service life of the equipment, and the reaction space is small, and the production efficiency of methanol is low. CONTENT OF THE UTILITY MODEL
[0004] Therefore, the present application provides a methanol synthesis reactor to solve or improve the problem of low methanol production efficiency.
[0005] The present application provides a methanol synthesis reactor, comprising:
[0006] A shell, the inner cavity of which is provided with a first partition plate and a second partition plate, the first partition plate and the second partition plate sequentially divide the inner cavity of the shell into a feeding cavity, a reaction cavity and a discharging cavity along a first direction, the first partition plate is provided with a first through hole, the second partition plate is provided with a second through hole, the shell is provided with a feeding port communicating with the feeding cavity, a discharging port communicating with the discharging cavity, a cooling liquid inlet and a cooling liquid outlet communicating with the reaction cavity;
[0007] A spiral pipe assembly is located in the reaction cavity, one end of the spiral pipe assembly communicates with the first through hole respectively, and the other end communicates with the second through hole;
[0008] A catalyst is arranged in the spiral pipe assembly, and a gas passing gap is formed between the spiral pipe assembly and the catalyst;
[0009] A catalyst blocking piece is located in the discharging cavity and connected with the second partition plate, and a plurality of gas permeable holes are formed in the catalyst blocking piece.
[0010] In this embodiment, the catalyst is transported from the feeding port to the feeding cavity and falls on the first partition plate. The catalyst enters the inside of the spiral pipe assembly from the first through hole, and a gas passing gap is formed between the catalyst and the spiral pipe. The catalyst blocking piece can prevent the catalyst from falling from the spiral pipe assembly into the discharging cavity, so as to ensure that the catalyst is always in the spiral pipe assembly and performs catalytic action.
[0011] The cooling liquid enters the reaction cavity from the cooling liquid inlet, so that the spiral pipe assembly is immersed in the cooling liquid, and the cooling liquid is output from the cooling liquid outlet, so as to ensure the flowability of the cooling liquid and maintain the working temperature of the cooling liquid.
[0012] The spiral pipe assembly is spirally installed in the reaction cavity. Compared with the space in the straight pipe, the spiral pipe assembly can accommodate more catalysts and prolong the reaction path, thereby improving the reaction efficiency and the production efficiency of methanol.
[0013] In addition, due to thermal expansion and contraction, the stress generated in the first direction of the spiral pipe assembly is smaller than the pipeline thermal stress generated in the straight pipe, thereby reducing the damage to the equipment.
[0014] In an alternative embodiment, the spiral pipe assembly comprises a plurality of layers of spiral pipe bundles arranged coaxially, and the plurality of layers of spiral pipe bundles are arranged radially at intervals, and the spiral directions of the spiral pipe bundles of adjacent layers are opposite.
[0015] One end of each of the plurality of layers of spiral pipe bundles communicates with the first through hole, and the other end of each of the plurality of layers of spiral pipe bundles communicates with the second through hole.
[0016] In an alternative embodiment, a plurality of fasteners are further included, and the plurality of fasteners are correspondingly connected to the plurality of layers of spiral pipe bundles.
[0017] In an alternative embodiment, each of the plurality of layers of spiral pipe bundles comprises a plurality of spiral pipes arranged at intervals in the circumferential direction, and the catalyst is arranged in the plurality of spiral pipes.
[0018] The first through hole and the second through hole are provided in plurality, one end of the plurality of spiral pipes respectively communicates with the plurality of first through holes, and the other end respectively communicates with the plurality of second through holes.
[0019] In an alternative embodiment, a plurality of first spheres are further included, the plurality of first spheres are located in the feeding cavity and stacked on the first partition plate, a first ventilation gap is formed between the plurality of first spheres, the first ventilation gap communicates with the plurality of first through holes, and the diameter of the first sphere is greater than the diameter of the first through hole.
[0020] In an alternative embodiment, the catalyst blocking member comprises:
[0021] A support cover provided with a plurality of ventilation holes, the support cover is located in the discharging cavity and covers the discharging port;
[0022] A barrier net connected to the support cover, and the mesh holes of the barrier net communicate with the ventilation holes;
[0023] A plurality of second spheres are stacked in the discharge cavity, and the plurality of second spheres close to the second partition plate can block the catalyst in the spiral pipe from falling into the discharge cavity, and a second ventilation gap is formed between the plurality of second spheres, which is in communication with the plurality of second through holes and the plurality of ventilation holes.
[0024] In an alternative embodiment, a plurality of baffles are arranged in the reaction cavity and connected to the inner wall of the shell.
[0025] In an alternative embodiment, an exhaust port is arranged on the shell and in communication with the reaction cavity, and the exhaust port is located between the cooling liquid outlet and the first partition plate in the first direction.
[0026] In an alternative embodiment, a first liquid level port and a second liquid level port are arranged on the shell and in communication with the reaction cavity, and the first liquid level port and the second liquid level port are connected by a liquid level tube.
[0027] In an alternative embodiment, a first temperature detection unit and a second temperature detection unit are further included, a temperature detection port is arranged on the middle part of the cavity wall of the reaction cavity in the first direction, the first temperature detection unit is installed on the temperature detection port, and the second temperature detection unit is arranged on the cooling liquid outlet.
[0028] The beneficial effects of the present application are as follows:
[0029] 1. The spiral pipe type heat exchanger is adopted, and the influence of thermal stress on the equipment can be effectively reduced by optimizing the structure and layout of the heat exchange pipe.
[0030] 2. The heat exchange pipe is filled with catalyst, and compared with the traditional straight pipe type pipe filling, the spiral pipe design significantly increases the loading amount of the catalyst and improves the load of the device.
[0031] 3. The heat of the heat exchange pipe is absorbed by water bath, and the cooling water is introduced into the shell through the cooling liquid inlet, which can absorb the heat of the reaction products in the spiral pipe. Since the synthesis of methanol is an exothermic reaction, the synthesis gas moves from top to bottom, and the working temperature is higher near the bottom. By using cooling water to exchange heat with the materials in the spiral pipe, the heat exchange efficiency is high, the heat exchange stability is good, and the situation that the heat-sensitive materials in the spiral pipe are deteriorated due to the direct heat exchange between the high-temperature saturated steam and the spiral pipe can be avoided, which increases the service life of the spiral pipe and further ensures the heat exchange effect and product quality.
[0032] 4. The cooling medium is cooling water, which can absorb the reaction heat and superheated steam to a great extent, thereby greatly reducing the temperature in the shell. The cooling water flows countercurrently from bottom to top, and a high-temperature region is not easy to form in the spiral pipe, so the heat transfer efficiency is high, and the thermal stress is greatly reduced due to the spiral structure.
[0033] 5. The catalyst in each spiral tube can operate under similar working conditions, thereby extending the catalyst's service life. If the spiral tube lengths differ too much, the heat release will differ. Overly long spiral tubes will have areas with significantly higher temperatures than other parts due to heat accumulation, which will affect the catalyst's lifespan.
[0034] 6. The spiral structure of the spiral tube enhances its ability to withstand high pressure.
[0035] 7. The shell has a vertical structure, which facilitates the loading and unloading of catalyst. Attached Figure Description
[0036] To more clearly illustrate the technical solutions in the specific embodiments of this application or the prior art, the drawings used in the description of the specific embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of this application. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.
[0037] Figure 1 This is a schematic diagram of the structure of a methanol synthesis reactor according to an embodiment of this application;
[0038] Figure 2 for Figure 1 A magnified view of part A in the diagram;
[0039] Figure 3 This is a schematic diagram of the discharge chamber in a methanol synthesis reactor according to an embodiment of this application.
[0040] Explanation of reference numerals in the attached figures:
[0041] 1. Shell; 2. First partition; 3. Second partition; 4. Feed chamber; 5. Reaction chamber; 6. Discharge chamber; 7. Catalyst barrier; 701 Support cover; 702. Second sphere; 8. Fastener; 9. Spiral tube; 10. Discharge port; 11. Coolant inlet; 12. Coolant outlet; 13. First sphere; 14. Baffle plate; 15. Exhaust port; 16. First liquid level port; 17. Second liquid level port; 18. Liquid level pipe; 19. Feed port; 20. Gas distributor; 21. Manhole; 22. Temperature detection port; 23. Catalyst discharge port; X, First direction. Detailed Implementation
[0042] To make the purposes, technical solutions, and advantages of the embodiments of the present application clearer, the technical solutions in the embodiments of the present application will be described clearly and completely below with reference to the drawings in the embodiments of the present application. Obviously, the described embodiments are some but not all of the embodiments of the present application. Based on the embodiments in the present application, all other embodiments obtained by a person of ordinary skill in the art without creative work fall within the protection scope of the present application.
[0043] The heat exchanger is a device for heat exchange of two or more fluids at different temperatures, which can transfer heat from the fluid at a higher temperature to the fluid at a lower temperature, so that the fluid temperature reaches the process specified index. It is widely used in petroleum, chemical, power, refrigeration and other industrial fields.
[0044] In the related art, Lurgi methanol reactors are used to prepare methanol. The Lurgi methanol reactor is a fixed tube plate heat exchanger, and the reaction tube is a straight tube. When the temperature rises to the highest temperature, the reaction force is difficult to eliminate, which easily causes damage to the equipment, affects the service life of the equipment, and the reaction space is small, and the production efficiency of methanol is low. In order to solve or improve the problem of low methanol production efficiency, the present application provides a methanol synthesis reactor.
[0045] The embodiments of the present application will be described below in combination with Figures 1 to 3 .
[0046] According to the embodiments of the present application, a methanol synthesis reactor is provided, as shown in Figure 1 , comprising: a shell 1, a spiral pipe assembly, a catalyst, and a catalyst blocking piece 7.
[0047] The inner cavity of the shell 1 is provided with a first partition plate 2 and a second partition plate 3, and the inner cavity of the shell 1 is sequentially divided into a feed cavity 4, a reaction cavity 5, and a discharge cavity 6 along a first direction X by the first partition plate 2 and the second partition plate 3. A first through hole is formed on the first partition plate 2, and a second through hole is formed on the second partition plate 3. A feed inlet 19 communicating with the feed cavity 4, a discharge outlet 10 communicating with the discharge cavity 6, a cooling liquid inlet 11 and a cooling liquid outlet 12 communicating with the reaction cavity 5 are formed on the shell 1;
[0048] The spiral pipe assembly is located in the reaction cavity 5, and one end of the spiral pipe assembly communicates with the first through hole and the other end communicates with the second through hole;
[0049] The catalyst is arranged in the spiral pipe assembly, and a gas passing gap is formed between the spiral pipe assembly and the catalyst;
[0050] The catalyst blocking piece 7 is located in the discharge cavity 6 and connected with the second partition plate 3, and a plurality of gas permeable holes are formed on the catalyst blocking piece 7.
[0051] In this embodiment, the catalyst is transported from the feed inlet 19 to the feed cavity 4 and falls on the first partition plate 2, the catalyst enters the inside of the spiral pipe assembly from the first through hole, a gas passing gap is formed between the catalyst and the spiral pipe 9, the catalyst blocking piece 7 can prevent the catalyst from falling from the spiral pipe assembly into the discharge cavity 6, and the catalyst is ensured to be always in the spiral pipe assembly to perform catalysis.
[0052] The cooling liquid enters the reaction cavity 5 from the cooling liquid inlet 11, so that the spiral pipe assembly is immersed in the cooling liquid, and the cooling liquid is output from the cooling liquid outlet 12, so as to ensure the flowability of the cooling liquid and maintain the working temperature of the cooling liquid.
[0053] The spiral pipe assembly is spirally installed in the reaction cavity 5, the space in the spiral pipe assembly is larger than that in a straight pipe, more catalysts can be accommodated, the reaction path is prolonged, the reaction efficiency is improved, and the production efficiency of methanol is improved.
[0054] In addition, due to thermal expansion and contraction, the stress generated by the spiral pipe assembly along the first direction X is smaller than the pipe thermal stress generated by a straight pipe, and the damage to the equipment is reduced.
[0055] Specifically, the catalyst is a copper-based catalyst, and the catalyst can be block-shaped, spherical or columnar.
[0056] Specifically, the catalyst is columnar, the diameter of the catalyst is 1mm to 5mm, and the height is 3mm to 10mm.
[0057] Specifically, the spiral angle of the spiral pipe assembly is 10° to 30°.
[0058] Specifically, a gas distributor is arranged on the feed inlet 19, and the methanol synthesis gas enters the feed cavity 4 through the gas distributor, and the gas distributor can preliminarily and uniformly distribute the methanol synthesis gas entering the feed cavity 4.
[0059] Specifically, the methanol synthesis gas includes multiple components.
[0060] Specifically, a manhole 21 is arranged on the shell 1, and a sealing cover is rotatably connected to the outer wall of the shell 1 to seal the manhole 21, and the manhole 21 can also be used for equipment maintenance.
[0061] Specifically, the catalyst can be transported into the feed cavity 4 through the manhole 21.
[0062] Specifically, the shell 1 is cylindrical.
[0063] Specifically, the material of the first partition plate 2 and the second partition plate 3 is 20MnMo IV + cladding S31803, wherein 20MnMo is a steel material, IV represents the grade of steel forgings, which means that the 20MnMo steel forgings of grade IV are cladded with S31803 (dual-phase steel) on the basis of the material to improve the ability to resist stress corrosion and chloride ion corrosion.
[0064] Specifically, the fixing mode of the spiral pipe 9 and the first partition plate 2 and the second partition plate 3 is strength welding + expansion bonding, which means that expansion bonding and welding are used together.
[0065] In one embodiment, as shown in Figure 1 , the spiral pipe assembly comprises a plurality of layers of coaxially arranged spiral pipe bundles, the plurality of layers of spiral pipe bundles are arranged radially spaced apart, and the spiral directions of the spiral pipe bundles of adjacent layers are opposite;
[0066] One end of each of the plurality of layers of spiral pipe bundles is in communication with the first through hole, and the other end of each of the plurality of layers of spiral pipe bundles is in communication with the second through hole.
[0067] In this embodiment, as shown in Figure 1 , the plurality of layers of coaxially arranged spiral pipe bundles are arranged spaced apart, facilitating the passage of the cooling liquid, the spiral directions of the spiral pipe bundles of adjacent layers are opposite, which can improve the turbulence degree of the cooling liquid in the reaction cavity 5, reduce the temperature difference of the cooling liquid at each position in the reaction cavity 5, and provide a good temperature environment for the reaction carried out in the spiral pipe bundle.
[0068] Specifically, the diameter of the spiral pipe bundle is 15 mm to 50 mm.
[0069] In one embodiment, as shown in Figure 1 , a plurality of fasteners 8 are further included, and the plurality of fasteners 8 are correspondingly connected to the plurality of layers of spiral pipe bundles.
[0070] In this embodiment, the plurality of fasteners 8 are correspondingly connected to the plurality of layers of spiral pipe bundles, preventing the spiral pipe bundles from being affected by thermal expansion and cold shrinkage, expanding radially, and being pressed by adjacent spiral pipe bundles, thereby causing damage to the spiral pipe bundles, so as to ensure that the thermal stress form of the spiral pipe bundles is mainly axial thermal stress.
[0071] Specifically, the contact surface of the fastener 8 and the spiral pipe bundle can be a smooth surface or a convex structure, and the contact part tightly engages the spiral pipe bundle, thereby slowing down the radial thermal stress of the spiral pipe bundle.
[0072] In one embodiment, as shown in Figure 1 , each layer of spiral pipe bundle comprises a plurality of spiral pipes 9, the plurality of spiral pipes 9 are arranged circumferentially spaced apart, and the catalyst is arranged in the plurality of spiral pipes 9;
[0073] The first and second through holes are provided in plurality, one end of the plurality of spiral tubes 9 is communicated with the plurality of first through holes respectively, and the other end is communicated with the plurality of second through holes respectively.
[0074] In this embodiment, the plurality of spiral tubes 9 are arranged at intervals, facilitating the flow of the cooling liquid. The spiral tube 9 is spirally installed in the reaction cavity 5, the space in the spiral tube 9 is larger than that in the straight tube, more catalysts can be accommodated, the reaction path is prolonged, the reaction efficiency is improved, and the production efficiency of methanol is improved.
[0075] Moreover, due to thermal expansion and contraction, the stress generated by the spiral tube 9 along the first direction X is smaller than the pipeline thermal stress generated by the straight tube, and the damage to the equipment is reduced.
[0076] Specifically, the spacing between the two adjacent spiral tubes 9 of the same layer of spiral tube bundle is 1mm to 2mm.
[0077] Specifically, the length of the spiral tube 9 is 2000mm to 8000mm.
[0078] In some embodiments, the maximum difference between the plurality of spiral tubes 9 does not exceed 1000mm, so that the heat generated by each spiral tube 9 is more balanced, preventing the problem of hot spot temperature rise.
[0079] Specifically, the pitch of the adjacent two turns of the spiral tube 9 is the same.
[0080] Specifically, the spiral tube 9 adopts a light pipe, a circular pipe, a threaded pipe, a twisted pipe or a wave pipe, and is preferably a light pipe.
[0081] Specifically, one end of the plurality of spiral tubes 9 is connected to the plurality of first through holes in a plug-in sealing manner, and the other end is connected to the plurality of second through holes in a plug-in sealing manner, and the first partition plate 2 and the second partition plate 3 can fix the spiral tube 9.
[0082] The spiral structure of the spiral tube 9 enhances the bearing capacity of high pressure, and also increases the rigidity and stability of the pipe wall, effectively reducing the deformation and stress concentration caused by high pressure. The spiral tube 9 can maintain good mechanical properties and long service life in a high-pressure environment, thereby improving the safety and reliability of the entire system.
[0083] Specifically, compared with the conventional fixed tube plate column tube arrangement scheme, the spiral tube 9 can obviously increase the heat exchange area, simplify the overall structure, reduce the overall land occupation area of the equipment and reduce the cost.
[0084] Specifically, the helix angle of the spiral tube 9 is set to an angle of 10° or 20° or 30° with the vertical direction. When the methanol synthesis gas is continuously introduced, the cooling liquid in the reaction cavity 5 forms a spiral turbulent flow state, accelerating the heat exchange effect.
[0085] In one embodiment, as shown inFigure 1 and Figure 2 As shown, it also includes a plurality of first spheres 13, which are located in the feed chamber 4 and stacked on the first partition 2. A first ventilation gap is formed between the plurality of first spheres 13, and the first ventilation gap is connected to a plurality of first through holes. The diameter of the first sphere 13 is larger than the diameter of the first through hole.
[0086] In this embodiment, a first ventilation gap is formed between multiple first spheres 13. Methanol synthesis gas enters multiple spiral tubes 9 through the first ventilation gap. The multiple first spheres 13 can disperse the methanol synthesis gas, making the components in the methanol synthesis gas more uniform. The first spheres 13 can optimize the distribution of methanol synthesis gas in the axial and radial directions of the feed chamber 4, ensuring uniform flow of methanol synthesis gas in the feed chamber 4. This makes the amount of methanol synthesis gas entering each spiral tube 9 the same or similar, which not only improves the reaction efficiency but also improves the uniformity of methanol synthesis gas, further improving the quality and yield of the reaction products.
[0087] Specifically, the number of first spheres 13 can be adjusted to change the stacking height of multiple first spheres 13, thereby adjusting the uniformity of methanol synthesis gas after passing through multiple first spheres 13.
[0088] Specifically, the first sphere 13 is an alumina ceramic sphere, which is stable and does not participate in the reaction, thus helping to optimize the distribution of methanol synthesis gas.
[0089] Specifically, the outer diameter of the first sphere 13 should be 20mm to 30mm.
[0090] In one embodiment, such as Figure 3 As shown, the catalyst blocking component 7 includes: a support cover 701, a barrier net, and a plurality of second spheres 702. Specifically, the support cover 701 is provided with a plurality of vent holes, and the support cover 701 is located inside the discharge chamber 6 and covers the discharge port 10; the barrier net is connected to the support cover 701, and the mesh of the barrier net is connected to the vent holes; the plurality of second spheres 702 are piled up in the discharge chamber 6, and the plurality of second spheres 702 near the second partition 3 can prevent the catalyst in the spiral tube 9 from falling into the discharge chamber 6, and a second venting gap is formed between the plurality of second spheres 702, and the second venting gap is connected to a plurality of second through holes and a plurality of vent holes.
[0091] In this embodiment, the support cover 701 can support the barrier net and multiple second spheres 702. The outer wall of the support cover 701 and the inner wall of the discharge chamber 6 are filled with second spheres 702. The second spheres 702 are used to prevent the catalyst in the spiral tube 9 from falling into the discharge chamber 6. A second ventilation gap is formed between the multiple second spheres 702. The generated methanol gas is homogenized by the second ventilation gap to achieve the same density and purity, and is output from the discharge port 10 through the mesh and ventilation holes of the barrier net.
[0092] Specifically, the second spheres 702 are alumina ceramic spheres, which are stable in nature and do not participate in the reaction, and are used to block the catalyst in the spiral pipe 9.
[0093] Specifically, as shown in Figure 3 , the second spheres 702 are arranged in a first layer and a second layer along the first direction X, the second spheres 702 in the first layer are in contact with the second partition, and the diameter of the second spheres 702 in the first layer is smaller than that of the second spheres 702 in the second layer.
[0094] Specifically, the outer diameter of the second spheres 702 in the first layer is 5mm to 8mm, and the outer diameter of the second spheres 702 in the second layer is 20mm to 30mm.
[0095] Specifically, the opening rate of the support cover 701 should be 30% to 40%; the barrier net is a wire mesh or other material, the wire diameter is 0.8mm to 1.2mm, and the mesh size is 0.4mm to 0.6mm.
[0096] Specifically, the shell 1 is provided with a catalyst discharge port 23 communicating with the discharge chamber 6, and the support cover 701, the barrier net and the plurality of second spheres 702 can be installed and removed from the catalyst discharge port 23, which is conducive to taking out the catalyst.
[0097] Specifically, the catalyst discharge port 23 is provided with two, and is located on both sides of the discharge port 10.
[0098] In one embodiment, as shown in Figure 1 , it further comprises a plurality of baffles 14, which are located in the reaction chamber 5 and connected to the inner wall of the shell 1.
[0099] In this embodiment, the baffles 14 can increase the turbulence of the cold zone liquid in the reaction chamber 5, reduce the temperature difference of the cooling liquid in the reaction chamber 5 in the axial and radial directions, improve the stability of the reaction environment, provide a good temperature environment for the reaction in the spiral pipe 9, and ensure that the axial temperature difference in the reaction chamber 5 is not more than 20℃, and the temperature difference in the same plane is not more than 5℃. Improve the uniformity and consistency of the reaction, and improve the quality and performance of the final product. By optimizing the temperature distribution, the baffles 14 help to reduce the problem of local overheating and large temperature gradient, ensure more accurate temperature control during the whole reaction process, so as to realize higher reaction efficiency and better product quality.
[0100] Specifically, the distance between the plurality of baffles 14 gradually increases in the direction from the discharge chamber 6 to the feed chamber 4.
[0101] In one embodiment, as shown in Figure 1As shown, the shell 1 is provided with an exhaust port 15, which is in communication with the reaction cavity 5, and is located between the cooling liquid outlet 12 and the first partition plate 2 along the first direction X.
[0102] In this embodiment, the exhaust port 15 is kept open during the process that the cooling liquid enters the reaction cavity 5 through the cooling liquid inlet 11, until the gas in the reaction cavity 5 is completely exhausted, so as to ensure that the water level of the cooling liquid reaches the designated position, which can avoid the pressure fluctuation in the reaction cavity 5 caused by the gas accumulation, ensure the stable operation of the system, and improve the safety.
[0103] In one embodiment, as shown in the accompanying drawings, Figure 1 The shell 1 is provided with a first liquid level port 16 and a second liquid level port 17, which are connected by a liquid level pipe 18.
[0104] In this embodiment, it is convenient to observe the height of the cooling liquid in the reaction cavity 5.
[0105] Specifically, the first liquid level port 16 is located below the cooling liquid inlet 11 along the first direction X, and the second liquid level port 17 is located above the cooling liquid outlet 12 along the first direction X.
[0106] In one embodiment, it further comprises a first temperature detection unit and a second temperature detection unit, and the cavity wall of the reaction cavity 5 is provided with a temperature detection port 22 at the middle part along the first direction X, the first temperature detection unit is installed at the temperature detection port 22, and the second temperature detection unit is arranged at the cooling liquid outlet 12.
[0107] In this embodiment, the temperature of the cooling liquid in the reaction cavity 5 and the temperature of the cooling liquid output are measured.
[0108] Specifically, 6 to 8 temperature sensors can be arranged on the spiral pipe 9 along the first direction X, and are connected with the temperature display, for detecting the temperature at different positions of the spiral pipe 9.
[0109] Next, an embodiment will be described in combination with Figures 1 to 3 to comprehensively describe all the above-mentioned solutions.
[0110] The worker fills the catalyst into the feed cavity 4 through the manhole 21, and fills the catalyst into the multiple spiral tubes 9 through the first through holes. Then the worker fills the multiple first balls 13 into the feed cavity 4, and the multiple first balls 13 are stacked on the first partition plate 2, and the first ventilation gaps are formed between the multiple first balls 13, and the first ventilation gaps are communicated with the multiple first through holes. The methanol synthesis gas enters the multiple spiral tubes 9 through the first ventilation gaps, and the methanol synthesis gas can be dispersed through the multiple first balls 13, so as to optimize the gas distribution of the feed cavity 4 in the axial and radial directions, and ensure the uniform flow of the methanol synthesis gas in the feed cavity 4, so that the amount of the methanol synthesis gas entering each spiral tube 9 is the same or similar.
[0111] The cooling liquid is introduced through the cooling liquid inlet 11, and the cooling liquid is filled in the reaction cavity 5, and the multiple spiral tubes 9 are immersed in the cooling liquid. During the process of filling the cooling liquid, the exhaust port 15 is kept open until the gas in the reaction cavity 5 is completely exhausted, and the water level of the cooling liquid reaches the specified position, so as to avoid the pressure fluctuation in the reaction cavity 5 caused by the gas accumulation, ensure the stable operation of the system, and improve the safety.
[0112] The methanol synthesis exchanges heat with the material through the water bath mode. After the cooling liquid is introduced into the reaction cavity 5 through the cooling liquid inlet 11, the cooling liquid can exchange heat with the material in the spiral tube 9, so as to keep the temperature of the material at the optimal working temperature. The material in the spiral tube 9 is uniformly exchanged by the cooling liquid, and the heat exchange efficiency is high and the heat exchange stability is good.
[0113] The methanol synthesis reactor can adapt to the small temperature difference working condition heat exchange, and when applied to the water bath type heat exchange working condition, the axial temperature difference can be reduced to a greater extent, and the working condition can be kept stable.
[0114] Compared with the traditional fixed tube plate column tube type arrangement scheme, the spiral tube 9 of the methanol synthesis reactor can obviously increase the heat exchange area, simplify the overall structure, reduce the overall land occupation area of the equipment, and reduce the cost.
[0115] When the methanol synthesis reactor is stably operated, the liquid level height in the liquid level pipe 18 is consistent with the liquid level height in the reaction cavity 5. The liquid level height in the reaction cavity 5 can be obviously known through the liquid level height in the liquid level pipe 18, and the flow of the cooling liquid inlet 11 can be adjusted according to the comparison of the liquid level height and the height of the cooling liquid outlet 12, so as to ensure the heat exchange effect and the product quality.
[0116] If the liquid level height in the liquid level pipe 18 is higher than the height of the cooling liquid outlet 12, the flow of the cooling liquid inlet 11 is reduced or the cooling liquid inlet 11 is closed until the liquid level height in the liquid level pipe 18 is consistent with the height of the cooling liquid outlet 12.
[0117] If the liquid level height in the liquid level pipe 18 is lower than the height of the cooling liquid outlet 12, the cooling liquid flow of the cooling liquid inlet 11 is increased until the liquid level height in the liquid level pipe 18 is consistent with the height of the cooling liquid outlet 12;
[0118] When the liquid level height in the liquid level pipe 18 is higher than the height of the cooling liquid outlet 12, it indicates that there is more cooling liquid in the reaction cavity 5, and the cooling liquid outlet 12 cannot discharge in time. At this time, the cooling liquid flow of the cooling liquid inlet 11 should be reduced or the cooling liquid inlet 11 should be directly closed. When the liquid level height in the liquid level pipe 18 is lower than the height of the cooling liquid outlet 12, it indicates that there is less cooling liquid in the reaction cavity 5. At this time, the cooling liquid flow of the cooling liquid inlet 11 should be appropriately increased. When the liquid level height of the liquid level pipe 18 is consistent with the height of the cooling liquid outlet 12, the flow of the cooling liquid inlet 11 is adjusted again so that the liquid level height of the liquid level pipe 18 and the height of the cooling liquid inlet 11 are maintained in a consistent state.
[0119] By setting the liquid level pipe 18, the cooling liquid flow of the cooling liquid inlet 11 is adjusted according to the liquid level height in the liquid level pipe 18 and the height of the cooling liquid outlet 12. The amount of cooling liquid in the reaction cavity 5 can be observed in real time, and the amount of cooling liquid is ensured to be sufficient to ensure that the cooling liquid can exchange heat with the material, thereby ensuring the heat exchange effect of the methanol synthesis reactor on the material, and at the same time ensuring that the methanol synthesis reactor can stably operate.
[0120] In order to facilitate observation of the liquid level height in the liquid level pipe 18, the liquid level pipe 18 can be set as a transparent pipe. Further, a scale corresponding to the height of the cooling liquid outlet 12 can be provided on the liquid level pipe 18 to facilitate observation of whether the liquid level height in the liquid level pipe 18 is higher than the height of the cooling liquid outlet 12.
[0121] Of course, the liquid level height in the reaction cavity 5 can also be detected by setting a liquid level gauge in the reaction cavity 5, and the detection result can be output to a terminal or a display device for observation. By detecting the liquid level height in the reaction cavity 5 through the liquid level pipe 18, the detection of the liquid level height in the reaction cavity 5 is facilitated, the overall structure is simplified, and the detection stability and service life are ensured.
[0122] The first temperature detection unit is used to detect the temperature value of the cooling liquid in the reaction cavity 5. Specifically, a temperature detection port 22 can be further provided in the middle side wall of the reaction cavity 5, and the first temperature detection unit is arranged in the temperature detection port 22. The middle position can be located at the middle position of the reaction cavity 5 along the first direction X, but not necessarily at the middle position in the overall height direction. Specifically, it can be in the middle, slightly above the middle, or slightly below the middle.
[0123] The second temperature detection unit is arranged at the cooling liquid outlet 12 and is used to detect the temperature value of the cooling liquid discharged from the cooling liquid outlet 12.
[0124] The first temperature detecting unit and the second temperature detecting unit are used to detect the temperature value of the cooling liquid in the reaction cavity 5, and determine whether the flow of the cooling liquid can meet the heat exchange requirement of the material. At the position where the second temperature detecting unit is located, there is a preset temperature.
[0125] The first case: when the temperature value of the cooling liquid detected by the second temperature detecting unit is lower than the preset temperature, it means that the amount of the cooling liquid can meet the heat exchange requirement of the material. When the temperature value detected by the second temperature detecting unit is higher than the preset temperature, it means that at this time, the amount of the cooling liquid cannot meet the heat exchange requirement of the material, and the amount of the cooling liquid needs to be appropriately increased until the temperature value detected by the second temperature detecting unit is maintained at the preset temperature.
[0126] The second case: if the temperature value detected by the second temperature detecting unit is lower than the preset temperature, the flow of the methanol synthesis gas at the feeding port 19 is increased until the temperature value reaches the preset temperature. If the temperature value is higher than the preset temperature, the flow of the methanol synthesis gas at the feeding port 19 is reduced or the feeding port 19 is closed until the temperature value reaches the preset temperature.
[0127] It should be noted that the gas flow rate of the methanol synthesis gas has an optimal flow rate value, and there is an optimal flow corresponding to it. When adjusting, the flow of the cooling liquid inlet 11 is preferentially selected.
[0128] For different height positions in the reaction cavity 5, there can be different preset temperatures, which can be obtained by test, simulation, calculation, etc., and are not limited specifically herein. Moreover, the preset temperature can be a specific value or a temperature range.
[0129] Through the setting of the first temperature detecting unit and the second temperature detecting unit, and according to the temperature value of the cooling liquid detected by the first temperature detecting unit and the second temperature detecting unit, the flow of the cooling liquid at the cooling liquid inlet 11 is adjusted, so that the temperature of the cooling liquid in the reaction cavity 5 can be controlled in real time, and it is ensured that the cooling liquid can exchange sufficient heat to make the material maintain the optimal working temperature, thereby ensuring the heat exchange effect of the methanol synthesis reactor on the material.
[0130] The cooling liquid inlet 11 can be designed according to the heat required by the material, such as calculating the heat load according to the reaction heat of the material, calculating the required cooling liquid flow according to the heat load, and designing the cooling liquid inlet 11 of appropriate specifications according to the flow of the methanol synthesis gas, so as to ensure that sufficient cooling liquid can pass into the reaction cavity 5.
[0131] The methanol synthesis reactor is described in detail by taking the example that the methanol synthesis reactor exchanges heat with the methanol synthesis gas and the reaction product, and the reaction product is discharged from the discharging port 10.
[0132] In the methanol synthesis condition, the temperature of the feed inlet 19 is 200 DEG C, the temperature of the discharge outlet 10 is 270 DEG C, the working pressure of the synthesis gas in the spiral pipe 9 is 8-10 MPaG, the preset temperature of the cooling liquid according to the water bath type design requirement is 200 DEG C, and the working pressure of the cooling liquid is 4-6 MPaG.
[0133] The cooling liquid inlet 11 is opened, the cooling liquid is introduced into the reaction cavity 5 from the cooling liquid inlet 11, the cooling liquid exchanges heat with the spiral pipe 9, and until the second temperature detection unit detects that the temperature value of the cooling liquid in the reaction cavity 5 reaches the preset temperature 220 DEG C.
[0134] During the heat exchange process, the temperature value of the cooling liquid is monitored in real time by the second temperature detection unit, if the temperature value is higher than 240 DEG C, the cooling liquid flow is increased or the methanol synthesis gas flow is reduced, if the temperature value is lower than 220 DEG C, the methanol synthesis gas flow is increased or the cooling liquid flow is reduced. After adjustment, the temperature value detected by the second temperature detection unit is maintained at about 220 DEG C.
[0135] Increasing or reducing the cooling liquid flow refers to increasing or reducing the cooling liquid introduction flow of the cooling liquid inlet 11, and increasing or reducing the gas flow of the methanol synthesis gas refers to increasing or reducing the methanol synthesis gas introduction flow of the feed inlet 19.
[0136] The shell 1 is provided with a catalyst discharge port 23 communicating with the discharge cavity 6, the support cover 701, the barrier net and the plurality of second spheres 702 can be installed and removed from the catalyst discharge port 23, which is beneficial to the catalyst removal.
[0137] Although the embodiments of the application are described in conjunction with the drawings, various modifications and changes can be made by those skilled in the art without departing from the spirit and scope of the application, and such modifications and changes fall within the scope defined by the appended claims.
Claims
1. A methanol synthesis reactor, characterized in that, include: The shell (1) has a first partition (2) and a second partition (3) in its inner cavity. The first partition (2) and the second partition (3) divide the inner cavity of the shell (1) into a feeding chamber (4), a reaction chamber (5) and a discharging chamber (6) in sequence along a first direction (X). The first partition (2) has a first through hole, and the second partition (3) has a second through hole. The shell (1) has a feeding port (19) that connects to the feeding chamber (4), a discharging port (10) that connects to the discharging chamber (6), and a coolant inlet (11) and a coolant outlet (12) that connect to the reaction chamber (5). A spiral tube assembly is located inside the reaction chamber (5). One end of the spiral tube assembly is connected to the first through hole, and the other end is connected to the second through hole. A catalyst is disposed within the helical tube assembly, and a gas passage gap is formed between the helical tube assembly and the catalyst. The catalyst blocking component (7) is located inside the discharge chamber (6) and connected to the second partition (3). The catalyst blocking component (7) has multiple air vents.
2. The methanol synthesis reactor according to claim 1, characterized in that, The helical tube assembly includes multiple layers of coaxially arranged helical tube bundles, which are arranged radially spaced apart, with adjacent layers having opposite helical directions. One end of each of the multi-layered spiral tube bundles is connected to the first through hole, and the other end of each of the multi-layered spiral tube bundles is connected to the second through hole.
3. The methanol synthesis reactor according to claim 2, characterized in that, It also includes a plurality of fasteners (8), which are correspondingly connected to the multilayer spiral tube bundle.
4. The methanol synthesis reactor according to claim 2, characterized in that, Each layer of the spiral tube bundle includes multiple spiral tubes (9), which are arranged circumferentially at intervals, and the catalyst is disposed within the multiple spiral tubes (9); Multiple first through holes and multiple second through holes are provided. One end of each of the multiple spiral tubes (9) is connected to multiple first through holes, and the other end is connected to multiple second through holes.
5. The methanol synthesis reactor according to claim 4, characterized in that, It also includes a plurality of first spheres (13), which are located in the feed chamber (4) and stacked on the first partition (2). A first ventilation gap is formed between the plurality of first spheres (13), which communicates with the plurality of first through holes. The diameter of the first spheres (13) is larger than the diameter of the first through holes.
6. The methanol synthesis reactor according to claim 4, characterized in that, The catalyst blocking element (7) includes: The support cover (701) is provided with multiple ventilation holes. The support cover (701) is located inside the discharge chamber (6) and covers the discharge port (10). A barrier net is connected to the support cover (701), and the mesh of the barrier net is in communication with the vent hole; Multiple second spheres (702) are piled up in the discharge chamber (6). The multiple second spheres (702) near the second partition (3) can prevent the catalyst in the spiral tube (9) from falling into the discharge chamber (6). A second ventilation gap is formed between the multiple second spheres (702). The second ventilation gap is connected to multiple second through holes and multiple ventilation holes.
7. The methanol synthesis reactor according to claim 1, characterized in that, It also includes multiple baffles (14), which are located inside the reaction chamber (5) and connected to the inner wall of the housing (1).
8. The methanol synthesis reactor according to claim 1, characterized in that, The housing (1) is provided with an exhaust port (15), which is connected to the reaction chamber (5). Along the first direction (X), the exhaust port (15) is located between the coolant outlet (12) and the first partition (2).
9. The methanol synthesis reactor according to claim 1, characterized in that, The housing (1) has a first liquid level port (16) and a second liquid level port (17) that communicate with the reaction chamber (5). The first liquid level port (16) and the second liquid level port (17) are connected by a liquid level pipe (18).
10. The methanol synthesis reactor according to claim 1, characterized in that, It also includes a first temperature detection unit and a second temperature detection unit. A temperature detection port (22) is provided in the middle of the cavity wall of the reaction chamber (5) along the first direction (X). The first temperature detection unit is installed in the temperature detection port (22), and the second temperature detection unit is provided in the coolant outlet (12).