Methanol reactor
By loading the catalyst outside the heat exchanger tube in the methanol reactor and adopting a tubeless structure and syngas preheating technology, the problems of low catalyst loading coefficient and large volume are solved, achieving efficient and low-cost methanol production.
Patent Information
- Application Number
- CN202423281708.7
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-12-30
- Publication Date
- 2025-12-23
- Estimated Expiration
- 2034-12-30
AI Technical Summary
Existing methanol reactors have low catalyst loading coefficients, large volumes, low space utilization, and pose risks of leakage and high manufacturing difficulty.
The catalyst is packed on the outside of the heat exchanger tube and a tubeless structure is adopted. The syngas flows inside the heat exchanger tube for preheating and heat exchange, which reduces the heating temperature requirement of the upstream syngas. The uniformity of the syngas and the reaction efficiency are improved by the gas inlet distributor and the gas distribution zone.
It improves the catalyst loading coefficient, reduces reactor volume, lowers leakage risk and manufacturing difficulty, improves reaction efficiency and space utilization, and reduces energy consumption and equipment investment.
Smart Images
Figure CN223697689U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The present application relates to the technical field of methanol preparation, in particular to a methanol reactor. BACKGROUND
[0002] As a new emerging fuel, methanol has been paid more and more attention in recent years. The methanol reactor is one of the core equipments for preparing methanol by hydrogenating carbon dioxide. The methanol reactor in the prior art is usually a shell-and-tube water-cooled reactor. The catalyst is filled in the heat exchange tube of the reactor, and a cooling medium such as saturated boiling water is arranged outside the heat exchange tube. Since the catalyst is filled in the heat exchange tube, the catalyst filling coefficient of the shell-and-tube water-cooled reactor is low, and the volume is large. CONTENT OF THE UTILITY MODEL
[0003] Therefore, the present application provides a methanol reactor which can effectively improve the catalyst filling coefficient of the methanol reactor and reduce the volume of the methanol reactor.
[0004] In order to achieve the above-mentioned purpose, the present application provides the following technical scheme:
[0005] One, comprising:
[0006] The shell is provided with an inner cavity and a gas inlet and a gas outlet which are in communication with the inner cavity;
[0007] The catalyst bed is arranged in the inner cavity;
[0008] The heat exchange sleeve is connected with the gas inlet, and at least part of the heat exchange sleeve is wrapped by the catalyst bed, so that the heat exchange sleeve is installed in the shell by the support of the catalyst bed and the connection with the gas inlet;
[0009] The heat exchange sleeve is in communication with the catalyst bed, so that the gas entering the gas inlet can flow into the catalyst bed after flowing through the heat exchange sleeve. The catalyst bed is in communication with the gas outlet, so that the reacted gas can flow out of the catalyst bed and be discharged through the gas outlet.
[0010] Optionally, the heat exchange sleeve comprises an inner tube and an outer tube, the outer tube is sleeved outside the inner tube, and there is an annular gap between the inner tube and the outer tube:
[0011] The first end of the inner tube is connected with the gas inlet, the outer tube surrounds at least part of the inner tube, the inner tube is in communication with the annular gap, and the annular gap is in communication with the catalyst bed, so that the gas entering the gas inlet can flow into the catalyst bed after sequentially flowing through the inner tube and the annular gap.
[0012] Optionally, along the center line direction of the shell, the gas inlet and the gas outlet are distributed at two ends of the shell.
[0013] The inner tube, the outer tube and the annular gap all extend along the centerline direction of the shell, the inner tube extends from one end of the outer tube to the other end, the second end of the inner tube away from the gas inlet is in communication with the annular gap, and the part of the annular gap adjacent to the gas inlet is in communication with the catalyst bed.
[0014] Optionally, the methanol reactor further comprises a gas inlet distributor, the gas inlet distributor comprises an inlet and a plurality of outlets, the inlet of the gas inlet distributor is connected with the gas inlet, and the number of the heat exchange sleeves is plural, and the plurality of heat exchange sleeves are connected with the plurality of outlets of the gas inlet distributor one by one, so that the heat exchange sleeves are connected with the gas inlet through the gas inlet distributor.
[0015] Optionally, the gas inlet is located at the top of the shell, the gas outlet is located at the bottom of the shell, along the centerline direction of the shell, the catalyst bed occupies part of the inner cavity, the inner cavity forms a gas distribution area in the region adjacent to the gas inlet, and the part of the annular gap adjacent to the gas inlet is located in the gas distribution area, so that the gas flowing out of the annular gap can be distributed in the gas distribution area and then flow into the catalyst bed.
[0016] Optionally, the inner tube and the outer tube can move relative to each other along the centerline direction of the shell.
[0017] Optionally, the heat exchange sleeve further comprises a plurality of supports distributed in the circumferential direction of the annular gap, each of the supports is fixed to one of the outer wall of the inner tube and the inner wall of the outer tube and abuts the other.
[0018] Optionally, along the centerline direction of the shell, the support comprises a first end and a second end, the width of the first end in the radial direction of the heat exchange sleeve is greater than the width of the second end in the radial direction of the heat exchange sleeve, and the first end abuts the other.
[0019] Optionally, the support is in a spiral shape, and / or the support is in a plate shape.
[0020] Optionally, the methanol reactor comprises a temporary fixing member, the temporary fixing member comprises an installed state and a free state, wherein:
[0021] In the installed state, the temporary fixing member is connected with the inner tube and the outer tube, and the inner tube and the outer tube are fixed relative to each other in the centerline direction of the shell.
[0022] In the free state, the temporary fixing member is separated from the heat exchange sleeve.
[0023] Optionally, an end of the outer tube away from the gas inlet is a closed end, the second end of the inner tube abuts against the closed end, and the support member is fixedly connected to an outer wall of the inner tube;
[0024] The temporary fixing member includes a fixing block and a threaded connecting member. The fixing block is provided with a first groove for accommodating a partial tube wall of the outer tube. A groove wall of the first groove is provided with a threaded hole in communication with a space in the groove. The threaded connecting member is threadedly connected with the threaded hole, and is used for locking or unlocking the fixing block and the outer tube. The fixing block is provided with a clamping space for accommodating a partial support member.
[0025] When the threaded connecting member locks the fixing block and the outer tube, and the partial support member is located in the clamping space, the support member limits the fixing block in the direction from the first end to the second end of the inner tube, and the temporary fixing member is in the installation state.
[0026] In the embodiment of the present application, the catalyst is filled in the outside of the heat exchange sleeve pipe. Compared with the prior art of filling the catalyst in the inside of the heat exchange pipe, the catalyst filling coefficient is increased (for example, in the prior art of the tubular shell water-cooled reactor, the catalyst is filled in the inside of the heat exchange pipe, the catalyst filling coefficient is about 30%, and in the methanol reactor of the embodiment of the present application, the catalyst is filled in the outside of the heat exchange sleeve pipe, the catalyst filling coefficient can reach 50% to 70%), the space utilization rate is high, the volume of the methanol reactor required for the same catalyst filling amount is small, and the occupied space is small. BRIEF DESCRIPTION OF DRAWINGS
[0027] In order to more clearly illustrate the technical solutions of the embodiments of the present application or the prior art, the drawings needed in the description of the embodiments or the prior art will be briefly introduced. Obviously, the drawings in the following description are only embodiments of the present application, and other drawings can be obtained by those skilled in the art without creative labor on the basis of the provided drawings.
[0028] Figure 1 A structural schematic diagram of the methanol reactor provided by the embodiment of the present application is shown in the figure;
[0029] Figure 2 A sectional view of the heat exchange sleeve pipe provided by the embodiment of the present application is shown in the figure;
[0030] Figure 3 A structural schematic diagram of the second end of the inner tube provided by the embodiment of the present application is shown in the figure;
[0031] Figure 4 A structural schematic diagram of the support member in a spiral shape provided by the embodiment of the present application is shown in the figure;
[0032] Figure 5 Front view (left) and right view (right) of the temporary fixing member provided in the embodiments of the present application;
[0033] Figure 6 Structural schematic view of the temporary fixing member provided in the embodiments of the present application;
[0034] Figure 7 Structural schematic view of the first arrangement mode of the heat exchange sleeve provided in the embodiments of the present application;
[0035] Figure 8 Structural schematic view of the second arrangement mode of the heat exchange sleeve provided in the embodiments of the present application;
[0036] Figure 9 Structural schematic view of the third arrangement mode of the heat exchange sleeve provided in the embodiments of the present application.
[0037] In Figures 1-9 , the present application provides a catalyst bed device, which comprises a shell, a gas inlet, a gas outlet, a catalyst loading port, a catalyst unloading port, a catalyst bed, a heat exchange sleeve, a temporary fixing member, an inlet gas distributor, an outlet gas distributor, an outlet baffle and an inert porcelain ball.
[0038] 100, shell; 110, gas inlet; 120, gas outlet; 130, gas distribution area; 140, catalyst loading port; 150, catalyst unloading port;
[0039] 200, catalyst bed;
[0040] 300, heat exchange sleeve; 310, inner tube; 311, opening; 320, outer tube; 321, blocking plate; 330, annular gap; 340, support member;
[0041] 400, inlet gas distributor;
[0042] 500, temporary fixing member; 510, fixing block; 511, first groove; 512, clamping space; 513, threaded hole; 520, threaded connecting member;
[0043] 610, inlet gas main pipe; 620, inlet gas branch pipe;
[0044] 700, temperature measuring port;
[0045] 800, outlet baffle;
[0046] 900, inert porcelain ball. DETAILED DESCRIPTION
[0047] 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 only part of the embodiments of the present application, rather than all the embodiments of the present application. Based on the embodiments in the present application, all the other embodiments obtained by those skilled in the art without creative labor fall within the protection scope of the present application.
[0048] The process of carbon dioxide hydrogenation to methanol is to convert waste carbon dioxide into valuable chemical raw materials through chemical methods, which is of great significance for controlling greenhouse gas emissions and mitigating global warming. At the same time, the process of carbon dioxide hydrogenation to methanol also provides a sustainable method for producing methanol.
[0049] Carbon dioxide to methanol has the following advantages.
[0050] Reducing carbon dioxide emissions: Carbon dioxide is one of the main greenhouse gases, and by hydrogenating carbon dioxide to produce methanol, this greenhouse gas can be recycled and converted into useful chemical raw materials, avoiding direct emission into the atmosphere, thereby reducing the greenhouse effect.
[0051] Manufacturing methanol: Methanol is an important chemical raw material, widely used in various fields, including the manufacture of plastics, resins, paints, detergents, etc. By hydrogenating carbon dioxide to produce methanol, sustainable production can be achieved.
[0052] Renewable energy: Methanol can be used as a clean energy source, complete combustion only produces carbon dioxide and water, and carbon dioxide can be recycled to produce methanol. Using carbon dioxide to prepare methanol can not only utilize waste carbon dioxide, but also obtain clean energy.
[0053] Addressing energy crisis: With the use of fossil fuels, energy is gradually depleted, and humans need to find new renewable energy sources. Carbon dioxide hydrogenation to methanol provides a possibility to convert waste into valuable energy.
[0054] As shown in Figures 1-9 The methanol reactor provided by the embodiments of the present application can be used for carbon dioxide hydrogenation to methanol, hydrogen and carbon dioxide react in the presence of a catalyst to generate methanol, and the reaction formula is as follows:
[0055]
[0056] The methanol reactor in the embodiments of the present application includes a shell 100, a catalyst bed 200, and a heat exchange sleeve 300.
[0057] The shell 100 is provided with an inner cavity, an inlet 110 and an outlet 120 which communicate with the inner cavity. The inlet 110 is the gas inlet, and the outlet 120 is the gas outlet. The gas in the embodiments of the present application can be synthesis gas (synthesis gas is a mixture of hydrogen and carbon dioxide, or a mixture mainly composed of hydrogen and carbon dioxide). The catalyst bed 200 is a catalyst particle layer composed of catalyst particles, and the catalyst bed 200 is arranged in the inner cavity.
[0058] The heat exchange sleeve 300 is connected with the gas inlet 110, so that the synthesis gas entering the methanol reactor through the gas inlet 110 can enter the heat exchange sleeve 300, and the catalyst bed 200 wraps at least part of the heat exchange sleeve 300, so that the heat exchange sleeve 300 can be installed in the shell 100 through the support of the catalyst bed 200 and the connection with the gas inlet 110.
[0059] The heat exchange sleeve 300 is in communication with the catalyst bed 200, so that the gas entering the gas inlet 110 can flow into the catalyst bed 200 after flowing through the heat exchange sleeve 300, the synthesis gas entering the catalyst bed 200 can be subjected to a synthesis reaction under the action of the catalyst (but the synthesis gas does not react with the catalyst, so the amount of the catalyst does not change during the reaction), and the catalyst bed 200 is in communication with the gas outlet 120, so that the gas (including methanol) after the synthesis reaction can flow out of the catalyst bed 200 and be discharged through the gas outlet 120. It should be noted that the synthesis gas entering the methanol reactor is synthesis gas with a certain pressure, so that the synthesis gas can flow in the methanol reactor, and the pressure of the synthesis gas entering the methanol reactor meets the pressure required for the synthesis reaction.
[0060] The synthesis reaction of the synthesis gas under the action of the catalyst releases heat, so that the temperature of the catalyst bed 200 after the synthesis reaction inside the synthesis gas is increased, and the temperature of the synthesis gas that is not preheated is lower than the temperature of the catalyst bed 200 after the synthesis reaction inside the synthesis gas. Therefore, during the flow of the synthesis gas in the heat exchange sleeve 300, the synthesis gas can exchange heat with the catalyst bed 200. In this case, the synthesis gas can be preheated to reach the temperature required for the synthesis reaction, and the reaction heat of the catalyst bed 200 can be removed without the need for other media to remove the reaction heat. Preheating the synthesis gas can reduce the heating temperature requirement of the synthesis gas upstream of the methanol reactor, thereby reducing the overall investment of the device. Removing the reaction heat of the catalyst bed 200 can prevent local overheating of the catalyst bed 200, maintain the optimal reaction conditions, reduce thermal stress, improve reaction efficiency, ensure operation safety, and ensure uniform and stable temperature of the catalyst bed 200.
[0061] It should be noted that during the initial period when the methanol reactor starts to work, the preheater can be provided upstream of the methanol reactor to preheat the synthesis gas before the synthesis gas enters the catalyst bed 200 and is subjected to a synthesis reaction under the action of the catalyst. After the temperature of the catalyst bed 200 reaches a preset value after the methanol reactor works for a preset time, the upstream preheater is closed. Specifically, the temperature of the catalyst bed 200 can be measured by a temperature detection device (such as a thermometer) installed in the temperature measuring port 700 (see below), and the upstream preheater is closed after the temperature reaches a preset value. After that, the synthesis gas is preheated by the reaction heat during the synthesis reaction of the synthesis gas under the action of the catalyst.
[0062] In the embodiment of the present application, the catalyst is filled outside the heat exchange sleeve 300. Compared with the prior art of filling the catalyst inside the heat exchange tube, the catalyst filling coefficient is increased (for example, in the prior art of the shell-and-tube water-cooled reactor, the catalyst is filled inside the heat exchange tube, the catalyst filling coefficient is about 30%, and in the methanol reactor of the embodiment of the present application, the catalyst is filled outside the heat exchange sleeve 300, the catalyst filling coefficient can reach 50% to 70%), the space utilization rate is high, the volume of the methanol reactor required for the same catalyst filling amount is small, and the occupied space is small.
[0063] In addition, in the prior art of the shell-and-tube water-cooled reactor, the tube-side medium is synthesis gas with a pressure of 5 to 10 MPa, and the shell-side medium is saturated water with a pressure of 2 to 4 MPa. The pressure difference between the tube and shell is large, the design is complex, the tube plate strength requirement is high, the thickness is large, the manufacturing difficulty is high, and the heat exchange tube bundle service life is short. In the methanol reactor of the embodiment of the present application, the internal medium is synthesis gas, therefore, the heat exchange sleeve 300 is not under pressure, and there is no need to set a tube plate, the manufacturing difficulty is low, and the cycle is short.
[0064] In the prior art of the shell-and-tube water-cooled reactor, a fixed tube plate structure is adopted, the heat exchange tube and the tube plate have many welded joints, the leakage possibility is high, and after the leakage, the tube and shell side media are contaminated with each other, and the reactor must be stopped for maintenance. In the methanol reactor of the embodiment of the present application, the heat exchange sleeve 300 is installed by using the catalyst bed 200 and the gas inlet 110, a tube plate-free structure is adopted, the leakage possibility is reduced, and in the methanol reactor, there is only one medium, i.e. synthesis gas, the internal parts are not under pressure, the leakage possibility is low, and after the leakage, other media will not be contaminated, and the internal parts have a simple structure.
[0065] In the prior art of the shell-and-tube water-cooled reactor, the synthesis gas needs to be preheated to a reaction temperature of about 210 to 250°C before entering the reactor, and the upstream synthesis gas heating temperature requirement is high. In the methanol reactor of the embodiment of the present application, when the synthesis gas flows in the heat exchange sleeve 300, the cold synthesis gas takes away the reaction heat generated by the reaction, and preheats the synthesis gas. The synthesis gas entering the methanol reactor only needs to be 150 to 190°C, the related synthesis gas preheating equipment investment can be reduced, and the energy consumption for preheating the synthesis gas can be significantly reduced.
[0066] There are various structures for realizing the above-mentioned gas flow path. In an alternative embodiment, the gas inlet 110 and the gas outlet 120 can be arranged at the top of the shell 100, the heat exchange sleeve 300 can extend in the vertical direction, and the end of the heat exchange sleeve 300 away from the gas inlet 110 can be covered with a mesh part. The synthesis gas can pass through the mesh holes of the mesh part, the mesh hole diameter of the mesh part is smaller than the diameter of the catalyst particles, so that the catalyst particles cannot pass through the mesh part, and the catalyst particles are prevented from entering the heat exchange sleeve 300.
[0067] In this structure, the synthesis gas enters the heat exchange sleeve 300 through the gas inlet 110, flows towards the port of the heat exchange sleeve 300 provided with the mesh, flows out through the mesh to the bottom layer of the catalyst bed 200, flows upwards in the catalyst bed 200 to the top layer of the catalyst bed 200, and flows out through the gas outlet 120 after fully contacting the catalyst bed 200 to occur the synthesis reaction under the action of the catalyst.
[0068] It should be noted that in this embodiment, the center line direction of the shell 100 is consistent with the vertical direction, and the top layer and the bottom layer of the catalyst bed 200 respectively refer to the top and the bottom of the catalyst bed 200 along the vertical direction, and the top of the shell 100 refers to the top of the shell 100 along the vertical direction.
[0069] In the embodiments of the present application, the heat exchange sleeve 300 can include an inner tube 310 and an outer tube 320, the outer tube 320 is sleeved outside the inner tube 310, and there is an annular gap 330 between the inner tube 310 and the outer tube 320. The first end of the inner tube 310 is connected with the gas inlet 110, the outer tube 320 surrounds at least part of the inner tube 310, the inner tube 310 communicates with the annular gap 330, and the annular gap 330 communicates with the catalyst bed 200, so that the gas entering the gas inlet 110 can flow into the catalyst bed 200 after sequentially flowing through the inner tube 310 and the annular gap 330.
[0070] In this structure, the heat exchange between the synthesis gas in the heat exchange sleeve 300 and the catalyst bed 200 has two processes, one is the heat exchange between the synthesis gas in the inner tube 310 and the synthesis gas in the annular gap 330, and the other is the heat exchange between the synthesis gas in the annular gap 330 and the catalyst bed 200. Through such a heat exchange process, on the one hand, the temperature difference of the synthesis gas in the annular gap 330 in the axial direction can be reduced, so that the temperature of the catalyst bed 200 is more uniform, and on the other hand, the flow velocity in the inner tube 310 and the annular gap 330 can be increased, and the increase of the flow velocity can increase the heat transfer coefficient and strengthen the heat transfer effect.
[0071] In the embodiments in which the heat exchange sleeve 300 includes the inner tube 310 and the outer tube 320, the inner tube 310 has a gas inlet end and a gas outlet end, and the annular gap 330 has a gas inlet area and a gas outlet area, and the synthesis gas sequentially flows through the gas inlet 110, the gas inlet end of the inner tube 310, the gas outlet end of the inner tube 310, the gas inlet area of the annular gap 330, the gas outlet area of the annular gap 330, and the gas outlet 120.
[0072] Since the synthesis reaction of the synthesis gas is exothermic, the temperature inside the shell 100 is high, and the synthesis gas entering the inside of the shell 100 absorbs the reaction heat and gradually increases the temperature. In this way, the temperature of the synthesis gas at the gas inlet end of the inner tube 310 is lower than the temperature of the synthesis gas at the gas outlet end of the inner tube 310, the temperature of the synthesis gas at the gas inlet area of the annular gap 330 is lower than the temperature of the synthesis gas at the gas outlet area of the annular gap 330, the gas inlet area of the annular gap 330 with a lower temperature exchanges heat with the gas outlet end of the inner tube 310 with a higher temperature, and the gas outlet area of the annular gap 330 exchanges heat with the gas inlet end of the inner tube 310, thereby reducing the temperature difference of the synthesis gas in the annular gap 330 in the axial direction, and the synthesis gas in the annular gap 330 with a uniform temperature distribution exchanges heat with the catalyst bed 200, which helps to make the temperature of the catalyst bed 200 more uniform.
[0073] The inner tube 310 divides the outer tube 320 into two areas, the space inside the inner tube 310 forms one area, and the annular gap 330 forms the other area. Compared with the case where the synthesis gas flows in the outer tube 320 without being divided into two areas, the structure of the heat exchange sleeve 300 including the inner tube 310 and the outer tube 320 reduces the flow area of the synthesis gas. Under the same flow rate and pressure, the smaller the flow area, the greater the flow rate. Therefore, the flow rate of the synthesis gas flowing in the inner tube 310 and the annular gap 330 increases, which increases the heat transfer coefficient and enhances the heat transfer effect.
[0074] In a further technical solution, the gas inlet 110 and the gas outlet 120 can be distributed at both ends of the shell 100 along the center line direction of the shell 100, the inner tube 310, the outer tube 320 and the annular gap 330 can extend along the center line direction of the shell 100, and the inner tube 310 extends from one end of the outer tube 320 to the other end, the second end of the inner tube 310 away from the gas inlet 110 communicates with the annular gap 330, and the part of the annular gap 330 adjacent to the gas inlet 110 communicates with the catalyst bed 200. This structure helps to lengthen the length of the annular gap 330 along the center line direction, lengthen the flow path of the synthesis gas in the heat exchange sleeve 300, and make the synthesis gas flow in the heat exchange sleeve 300 as far as possible, thereby improving the preheating effect of the synthesis gas and the removal effect of the reaction heat of the catalyst bed 200.
[0075] It should be noted that the center line direction of the shell 100 can be consistent with the vertical direction during the operation of the methanol reactor. The extension direction of the inner tube 310 and the outer tube 320 is the axial direction of the inner tube 310 and the outer tube 320, that is, the inner tube 310 and the outer tube 320 can be coaxially arranged, and the axial direction of the heat exchange sleeve 300 is consistent with the center line direction of the shell 100.
[0076] Specifically, an end of the outer tube 320 distal to the gas inlet 110 can be provided with a blocking plate 321, the blocking plate 321 blocks the port of the outer tube 320 distal to the gas inlet 110, the second end of the inner tube 310 can abut against the blocking plate 321, and the second end of the inner tube 310 can be provided with an opening 311, the inner tube 310 communicates with the annular gap 330 through the opening 311, so that the synthesis gas entering the heat exchange sleeve 300 can flow along the first end of the inner tube 310 to the second end, then flow into the part of the annular gap 330 distal to the gas inlet 110 through the opening 311, then flow along the annular gap 330, and finally flow into the catalyst bed 200 through the part of the annular gap 330 adjacent to the gas inlet 110.
[0077] Of course, in other alternative embodiments, the second end of the inner tube 310 can be opposite to the middle part (the middle part in the direction of the center line) of the outer tube 320; or, the gas inlet 110 of the shell 100 can be provided on the top of the shell 100, the gas outlet 120 can be provided on the side of the shell 100, the inner tube 310 and the outer tube 320 can both be designed as a spiral structure, and the inner tube 310 and the outer tube 320 are sleeved to form the heat exchange sleeve 300.
[0078] In the embodiments of the present application, the methanol reactor can further include a gas inlet distributor 400, the gas inlet distributor 400 includes an inlet and a plurality of outlets, the inlet of the gas inlet distributor 400 is connected with the gas inlet 110, the number of the heat exchange sleeves 300 is a plurality, and the first end of the inner tube 310 of the plurality of heat exchange sleeves 300 can be connected with the plurality of outlets of the gas inlet distributor 400 one by one through welding, so that the heat exchange sleeve 300 is connected with the gas inlet 110 through the gas inlet distributor 400. In this case, the number of the heat exchange sleeves 300 can be increased, thereby improving the working efficiency of the methanol reactor, and the uniform distribution of the synthesis gas through the gas inlet distributor 400 before entering the plurality of heat exchange sleeves 300 helps to improve the uniformity of the synthesis gas entering the catalyst bed 200.
[0079] The number of the gas inlet distributors 400 can be a plurality, the gas inlet 110 can be provided with a gas inlet main pipe 610, the gas inlet main pipe 610 can be connected with a plurality of gas inlet branch pipes 620, the plurality of gas inlet branch pipes 620 can be uniformly connected with the gas inlet main pipe 610, and the plurality of gas inlet distributors 400 can be connected with the plurality of gas inlet branch pipes 620 one by one, so that more heat exchange sleeves 300 can be installed, thereby further improving the working efficiency of the methanol reactor. The gas inlet 110, the gas inlet main pipe 610, the gas inlet branch pipe 620, and the gas inlet distributor 400 can be connected in sequence through welding, of course, they can also be connected through clamping and the like.
[0080] There are various distribution modes of the heat exchange sleeves 300, in an alternative embodiment, please refer again to Figure 7 andFigure 9 The methanol reactor can be arranged in a regular triangle, that is, the heat exchange sleeve 300 and the heat exchange sleeve 300 around it can be arranged in a regular triangle, wherein, Figure 7 The heat exchange sleeve 300 in the above embodiment is arranged in rows and columns, Figure 9 The heat exchange sleeve 300 in the above embodiment is arranged in concentric circles; please refer again to Figure 8 The methanol reactor can also be arranged in a square, that is, the heat exchange sleeve 300 and the heat exchange sleeve 300 around it can be arranged in a square. Of course, all the heat exchange sleeves 300 can also be arranged in other ways, which are not limited in this article.
[0081] In order to further improve the uniformity of the synthesis gas in the catalyst bed 200, the gas inlet 110 can be located at the top of the shell 100, and the gas outlet 120 can be located at the bottom of the shell 100. Along the center line direction of the shell 100, the catalyst bed 200 occupies part of the area of the inner cavity. The inner cavity forms a gas distribution area 130 in the area adjacent to the gas inlet 110. The gas distribution area 130 is free of catalyst particles. The part of the annular gap 330 adjacent to the gas inlet 110 is located in the gas distribution area 130, so that the gas flowing out of the annular gap 330 can be distributed in the gas distribution area 130 and then flow into the catalyst bed 200.
[0082] When the methanol reactor is working, the synthesis gas mainly composed of carbon dioxide and hydrogen enters the methanol reactor from the gas inlet 110. Inside the methanol reactor, the synthesis gas first passes through the gas inlet manifold 610 and the gas inlet branch pipe 620, and then flows into the gas inlet distributor 400. In the gas inlet distributor 400, the synthesis gas is first distributed and enters each heat exchange sleeve 300. The synthesis gas in the heat exchange sleeve 300 first passes through the inner pipe 310 downward to the second end of the inner pipe 310, and then enters the annular gap 330 between the inner pipe 310 and the outer pipe 320, flows upward to the outlet area of the annular gap 330, and then enters the top space of the methanol reactor, that is, the gas distribution area 130. In the gas distribution area 130, the synthesis gas is distributed again and then enters the catalyst bed 200 downward for reaction. The gas stream after reaction passes through the area where the inert porcelain balls 900 (see below) are located, and is discharged to the outside of the methanol reactor through the gas outlet 120.
[0083] In this structure, the synthesis gas enters the methanol reactor from the top inlet 110 and contacts the catalyst bed 200 twice during distribution, the first time by the gas distributor 400 located inside the methanol reactor, which distributes the synthesis gas from the inlet manifold 610 to each heat exchange sleeve 300; the second time is natural distribution, the preheated synthesis gas enters the gas distribution area 130 and is evenly distributed in the radial cross section. After two distributions, the synthesis gas in the methanol reactor is more evenly distributed, which makes the reaction heat in the methanol reactor more dispersed, which is beneficial to reduce the maximum temperature difference in the methanol reactor, which is beneficial to the temperature control of the methanol reactor and reduces the influence of temperature fluctuation on the catalyst.
[0084] The lower part of the catalyst bed 200 can be filled with inert porcelain balls 900 to support the catalyst bed 200.
[0085] In the above scheme, the heat exchange sleeve 300 includes an inner tube 310 and an outer tube 320, and in an optional embodiment, the inner tube 310 and the outer tube 320 can be fixedly connected, for example, can be connected by welding, or can be fixedly connected by bolt connection.
[0086] In the embodiment of the present application, the inner tube 310 and the outer tube 320 are movably fitted along the center line direction of the shell 100, that is, the inner tube 310 and the outer tube 320 can move relative to each other along the center line direction of the shell 100. In this case, when the temperature in the methanol reactor rises and the heat exchange sleeve 300 expands, the inner tube 310 and the outer tube 320 can move relative to each other, preventing the heat exchange sleeve 300 from being damaged due to the fixed connection between the two when thermal expansion occurs.
[0087] In addition, since the outer tube 320 is supported by the catalyst bed 200 and the inner tube 310 is fixed by being connected to the inlet 110, that is, the inner tube 310 and the outer tube 320 have no fixed connection relationship, when thermal expansion occurs, the inner tube 310 and the outer tube 320 can expand and contract simultaneously or independently, and the expansion and contraction amount can be the same or different, and there is no stress problem, therefore, the heat exchange sleeve 300 has lower requirements for material quality and can use ordinary 304 stainless steel material.
[0088] In a further technical solution, the heat exchange sleeve 300 can further comprise a plurality of supports 340 distributed along the circumference of the annular gap 330. In the direction of the center line of the heat exchange sleeve 300, the heat exchange sleeve 300 can also be provided with a plurality of supports 340 in the direction of the center line, and each support 340 is fixed to one of the outer wall of the inner tube 310 and the inner wall of the outer tube 320 and abuts the other. For example, the support 340 can be fixed to the outer wall of the inner tube 310 by welding or the like and abut the outer tube 320. In this way, the uniformity of the annular gap 330 can be ensured by providing the support 340, thereby making the distribution of the synthesis gas and heat exchange uniform.
[0089] In an alternative embodiment, the support 340 can be an equal-width structure in the radial direction (radial direction of the heat exchange sleeve 300).
[0090] In another alternative embodiment, in the direction of the center line of the shell 100, the support 340 can comprise a first end and a second end, the width of the first end in the radial direction of the heat exchange sleeve 300 can be greater than the width of the second end in the radial direction of the heat exchange sleeve 300, and the first end abuts the other. This structure is beneficial for the installation of the inner tube 310 and the outer tube 320, and is not easy to be stuck by the support 340 during the installation of the inner tube 310 and the outer tube 320, thereby reducing the assembly difficulty of the heat exchange sleeve 300.
[0091] The shape of the support 340 is various, please refer to Figure 4 , the support 340 can be spiral, the spiral support 340 can be an equal-width support 340 (of course, it can also be not equal-width), and the number of the spiral support 340 along the circumference of the heat exchange sleeve 300 can be two or more. The spiral support 340 not only can play the role of ensuring the uniformity of the annular gap 330, but also can increase the disturbance of the airflow in the annular gap 330, so as to make the temperature distribution of the synthesis gas uniform in the circumferential direction and the heat transfer effect better.
[0092] Please refer to Figure 2 , the support 340 can be plate-shaped, the plate-shaped support 340 can be a not-equal-width support 340, the number of the plate-shaped support 340 along the circumference of the heat exchange sleeve 300 can be three or more, and a plurality of (for example, two) plate-shaped supports 340 are provided in the direction of the center line (i.e., the axial direction) of the heat exchange sleeve 300.
[0093] In the embodiments of the present application, the supports 340 distributed along the circumference are taken as a group, each group comprises three or more supports 340, and each heat exchange sleeve 340 is distributed with two or more groups of supports 340 in the axial direction.
[0094] In the process of assembling the methanol reactor, it is difficult to insert the heat exchange sleeve 300 into the catalyst bed 200 after the catalyst is filled, therefore, in the process of assembling the methanol reactor of the embodiment of the present application, the heat exchange sleeve 300 can be first assembled into the shell 100, and then the catalyst is filled, since the inner tube 310 and the outer tube 320 can be relatively moved in the center line direction of the shell 100, therefore, in the process of assembling, the inner tube 310 and the outer tube 320 can be temporarily connected by means of the temporary fixing member 500 to prevent the relative movement of the inner tube 310 and the outer tube 320 in the axial direction.
[0095] The temporary fixing member 500 can include a mounted state and a free state, in the mounted state, the temporary fixing member 500 is connected with the inner tube 310 and the outer tube 320, so that the inner tube 310 and the outer tube 320 are relatively fixed in the center line direction, in the free state, the temporary fixing member 500 is separated from the heat exchange sleeve 300.
[0096] Specifically, the end of the outer tube 320 away from the gas inlet 110 is a blocked end (as described above, the blocked end is formed by blocking with the blocking plate 321), the second end of the inner tube 310 abuts against the blocked end, so that the inner tube 310 limits the outer tube 320 in the direction from the second end to the first end of the inner tube 310, after the inner tube 310 is connected with the gas inlet 110, the position of the inner tube 310 is relatively fixed, so that the outer tube 320 cannot move in the direction from the second end to the first end of the inner tube 310.
[0097] The temporary fixing member 500 can include a fixing block 510 and a threaded connecting member 520, the fixing block 510 can be a metal block, the threaded connecting member 520 can be a bolt, the fixing block 510 is provided with a first slot 511, the first slot 511 is used for accommodating part of the tube wall of the outer tube 320, the slot wall of the first slot 511 is provided with a threaded hole 513 in communication with the space in the slot, the threaded connecting member 520 is screwed with the threaded hole 513, used for locking or unlocking the fixing block 510 and the outer tube 320, the fixing block 510 is provided with a clamping space 512, the clamping space 512 is used for accommodating part of the support member 340.
[0098] In the case that the threaded connection 520 locks the fixing block 510 and the outer tube 320, and the partial support 340 is located in the clamping space 512, the support 340 is fixedly connected with the inner tube 310, the fixing block 510 is fixed with the outer tube 320, and the support 340 supports the outer tube 320 and the temporary fixing device 500, preventing the outer tube 320 from moving along the direction from the first end to the second end of the inner tube 310 under the action of its own gravity, so that the support 340 limits the fixing block 510 and the outer tube 320 in the direction from the first end to the second end of the inner tube 310. Therefore, the inner tube 310 and the support 340 limit the outer tube 320 in the direction from the first end to the second end of the inner tube 310, so that the inner tube 310 and the outer tube 320 are relatively fixed in the center line direction. At this time, the temporary fixing device 500 is in the installed state.
[0099] In order to facilitate the cooperation of the support 340 and the clamping space 512, the clamping space 512 can be a tapered structure, and the opening of the tapered structure is located on the surface of the slot opening of the first groove 511.
[0100] When connecting the inner tube 310 and the outer tube 320 by using the temporary fixing device 500, the first groove 511 can be clamped on the wall of the outer tube 320 first, and the threaded connection 520 is tightened, so that the threaded connection 520 abuts the wall of the outer tube 320 located in the first groove 511 against the groove wall of the first groove 511, thereby locking the fixing block 510 and the outer tube 320, and the partial support 340 is inserted into the clamping space, thereby completing the connection of the temporary fixing device 500 with the inner tube 310 and the outer tube 320.
[0101] The number of temporary fixing devices 500 can be the same as the number of circumferentially distributed supports 340, and they are connected one by one to improve the connection stability of the inner tube 310 and the outer tube 320 during the process of filling the catalyst.
[0102] After filling the inert porcelain balls 900 and the catalyst is completed, the threaded connection 520 can be rotated in the opposite direction to release the abutting relationship between the threaded connection 520 and the wall of the outer tube 320, thereby unlocking the fixing block 510 and the outer tube 320, so that the inner tube 310 and the outer tube 320 have a certain relative expansion and contraction, the temporary fixing device 500 is removed from the heat exchange sleeve 300, so that they are separated, and the temporary fixing device 500 is switched to the free state.
[0103] When the catalyst is loaded, a temporary auxiliary device can be used, which can be attached to the inner wall of the shell 100, and the catalyst particles can flow along the temporary auxiliary device, or the temporary auxiliary device can extend below the gas outlet area of the annular gap 330, and the catalyst particles can flow along the temporary auxiliary device to prevent the catalyst particles from entering the annular gap 330. A wire mesh can also be installed at the outlet area of the annular gap 330, and the mesh of the wire mesh can allow the synthesis gas to pass through but not the catalyst particles, so as to prevent the catalyst particles from entering the annular gap 330.
[0104] One or more temperature gauge sleeves can be provided in the catalyst bed 200, which are inserted into the catalyst bed 200, and a thermometer is connected in the temperature gauge sleeve. A temperature measuring port 700 is formed at the end of the temperature gauge sleeve outside the shell 100, which is used to detect the temperature of the catalyst bed 200. The temperature gauge sleeve can be fixed directly through the support of the catalyst bed 200, of course, it can also be connected to the shell 100 through the rib plate to realize the fixation of the temperature gauge sleeve. Whether the rib plate is needed to fix can be determined according to the length of the temperature gauge sleeve extending into the catalyst bed 200.
[0105] The bottom of the shell 100 is provided with a gas outlet 120, and the position of the gas outlet 120 can be covered with an outlet baffle 800. The outlet baffle 800 is used to block the inert porcelain balls 900 and the catalyst particles, so as to prevent the inert porcelain balls 900 and the catalyst particles from falling out of the methanol reactor through the gas outlet. The outlet baffle 800 is uniformly perforated, and the perforation can allow the reaction gas to pass through. A catalyst loading port 140 is provided above the catalyst loading area, which is used to load the catalyst into the shell 100 to form a catalyst bed 200 inside the shell 100. A catalyst unloading port 150 is provided below the catalyst loading area to discharge the catalyst particles.
[0106] Since the inner and outer operating media of the inner parts (including the gas inlet manifold 610, the gas inlet branch pipe 620, the gas distributor 400, the heat exchange sleeve 300 and the outlet baffle 800) of the methanol reactor of the embodiment of the application are all synthesis gas, the pressure difference is very small, and no pressure bearing is needed, so the inner parts have no high strength requirement, the manufacturing difficulty is low, and the cost is low. Secondly, the inner tube 310 and the outer tube 320 of the heat exchange sleeve 300 of the methanol reactor only need to be fixed at one end, and the other end can be freely expanded and contracted, and there is no problem of thermal expansion of the methanol reactor at high temperature. The material requirement is reduced and there is no need to set an expansion joint or other structure for balancing the temperature difference stress, so the inner parts of the methanol reactor in the embodiment of the application can use ordinary 304 stainless steel material, and the shell can use chromium-molybdenum steel.
[0107] A 100000 tons / year carbon dioxide hydrogenation to methanol device adopts the carbon dioxide hydrogenation to methanol reactor in the embodiment of the application. The reactor inlet temperature is about 160℃, the pressure is 8Mpa(G), the total flow of synthesis gas is about 250000Nm3 The main components in the synthesis gas are: hydrogen about 81%, carbon monoxide about 2%, carbon dioxide about 15%, nitrogen about 2%. The gas distributor 400 and the heat exchange sleeve 300 of the methanol reactor are made of S30408 material, the shell 100 of the methanol reactor is made of 15CrMoR material, the diameter of the methanol reactor is about 3.4m, the length of the heat exchange sleeve 300 is about 6m, and the catalyst loading is about 40m 3 The cost of the equipment is about 7.5 million yuan. During the reaction, the synthesis gas is preheated from 160℃ to 250℃ by the heat exchange sleeve 300 and enters the catalyst bed 200. The temperature of the catalyst bed 200 is stabilized at 245℃-255℃. The gas composition out of the methanol reactor is: hydrogen about 75%, carbon monoxide about 3%, carbon dioxide about 12%, nitrogen about 2%.
[0108] Under the same catalyst loading, if a shell-and-tube water-cooled reactor in the prior art is used, the diameter is about 3.8m, the length of the heat exchange tube is about 7.8m, and in order to overcome the temperature difference stress of the shell side, the thickness of the tube sheet is large, the heat exchange tube needs to be made of duplex steel, the cost of the reactor is about 9 million yuan, and a larger synthesis gas preheater is needed to preheat the gas flow entering the reactor to about 220℃.
[0109] Compared with the traditional shell-and-tube water-cooled reactor, the carbon dioxide hydrogenation to methanol reactor of the present application can realize the simplification of the process flow, the reduction of the device investment, the low cost of the reactor body, the small occupation of the land, the more reasonable use of the space, the high energy utilization rate of the reactor, and the obvious energy saving effect.
[0110] The above describes the basic principles of the present application in combination with specific embodiments, but it should be pointed out that the advantages, advantages, effects and the like mentioned in the present application are only examples and not limitations, and these advantages, advantages, effects and the like cannot be considered as the necessary possession of each embodiment of the present application. In addition, the above specific details are only for the purpose of example and understanding, and are not limited to the above specific details. The present application must be realized by using the above specific details.
[0111] The block diagrams of the devices, apparatuses, equipment, systems involved in the present application are only illustrative examples and are not intended to require or imply the connection, arrangement, configuration shown in the block diagram. As those skilled in the art will recognize, these devices, apparatuses, equipment, systems can be connected, arranged, configured in any way. Words such as "include", "contain", "have" and the like are open-ended words, which mean "include but not limited to", and can be used interchangeably. The words "or" and "and" used herein mean the word "and / or", and can be used interchangeably unless the context clearly indicates otherwise. The word "such as" used herein means the phrase "such as but not limited to", and can be used interchangeably.
[0112] It should also be noted that in the apparatus, devices and methods of the present application, the various components and steps are merely illustrative. Depending on the implementation, components and steps can be added or removed. Similarly, the ordering of the steps can be modified without departing from the scope of the present application.
[0113] The previous description of the disclosed aspects is provided to enable any person skilled in the art to make or use the application. Various modifications to these aspects will be readily apparent to those skilled in the art, and the generic principles defined herein can be applied to other aspects without departing from the scope of the application. Thus, the present application is not intended to be limited to the aspects shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
[0114] It should be understood that the limiting words "first", "second", "third", "fourth", "fifth" and "sixth" as used in the embodiments description of the present application are only used for the purpose of clearer explanation of the technical solutions, and cannot be used to limit the protection scope of the present application.
[0115] The above description has been presented for the purpose of illustration and description. Furthermore, this description is not intended to limit the embodiments of the application to the forms disclosed herein. Although several example aspects and embodiments have been discussed, it will be understood by those skilled in the art that certain modifications, variations, substitutions, additions and sub-combinations are possible.
Claims
1. A methanol reactor characterized in that, The methanol reactor comprises: a shell (100) provided with an inner cavity, an air inlet (110) and an air outlet (120) communicating with the inner cavity; a catalyst bed (200) arranged in the inner cavity; a heat exchange sleeve (300) connected with the air inlet (110), and at least part of the heat exchange sleeve (300) being wrapped by the catalyst bed (200) so that the heat exchange sleeve (300) is installed in the shell (100) by the support of the catalyst bed (200) and the connection with the air inlet (110); the heat exchange sleeve (300) communicates with the catalyst bed (200) so that the gas entering the air inlet (110) can flow into the catalyst bed (200) after flowing through the heat exchange sleeve (300), and the catalyst bed (200) communicates with the air outlet (120) so that the reacted gas can flow out of the catalyst bed (200) and be discharged through the air outlet (120).
2. The methanol reactor of claim 1, wherein, The heat exchange sleeve (300) comprises an inner tube (310) and an outer tube (320), the outer tube (320) is sleeved outside the inner tube (310), and there is an annular gap (330) between the inner tube (310) and the outer tube (320): a first end of the inner tube (310) is connected with the air inlet (110), the outer tube (320) surrounds at least part of the inner tube (310), the inner tube (310) communicates with the annular gap (330), and the annular gap (330) communicates with the catalyst bed (200) so that the gas entering the air inlet (110) can flow into the catalyst bed (200) after sequentially flowing through the inner tube (310) and the annular gap (330).
3. The methanol reactor of claim 2, wherein, The air inlet (110) and the air outlet (120) are distributed at two ends of the shell (100) along the center line direction of the shell (100); the inner tube (310), the outer tube (320) and the annular gap (330) all extend along the center line direction of the shell (100), the inner tube (310) extends from one end of the outer tube (320) to the other end, a second end of the inner tube (310) away from the air inlet (110) communicates with the annular gap (330), and a part of the annular gap (330) adjacent to the air inlet (110) communicates with the catalyst bed (200).
4. The methanol reactor of claim 3, wherein, The methanol reactor further comprises an air inlet distributor (400) comprising an inlet and a plurality of outlets, the inlet of the air inlet distributor (400) is connected with the air inlet (110), and a plurality of heat exchange sleeves (300) are connected with the plurality of outlets of the air inlet distributor (400) one by one so that the heat exchange sleeves (300) are connected with the air inlet (110) through the air inlet distributor (400).
5. The methanol reactor of claim 4, wherein, The air inlet (110) is located at the top of the shell (100), the air outlet (120) is located at the bottom of the shell (100), along the center line direction of the shell (100), the catalyst bed (200) occupies part of the inner cavity, the inner cavity forms a gas distribution area (130) in the area adjacent to the air inlet (110), and the part of the annular gap (330) adjacent to the air inlet (110) is located in the gas distribution area (130), so that the gas flowing out of the annular gap (330) can be distributed in the gas distribution area (130) and then flow into the catalyst bed (200).
6. The methanol reactor of claim 3, wherein, The inner tube (310) and the outer tube (320) can move relative to each other along the center line direction of the shell (100).
7. The methanol reactor of claim 6, wherein, The heat exchange sleeve (300) further comprises a plurality of supports (340) distributed along the circumference of the annular gap (330), each of the supports (340) is fixed to one of the outer wall of the inner tube (310) and the inner wall of the outer tube (320) and abuts the other.
8. The methanol reactor of claim 7, wherein, Along the center line direction of the shell (100), the support (340) comprises a first end and a second end, the width of the first end in the radial direction of the heat exchange sleeve (300) is greater than the width of the second end in the radial direction of the heat exchange sleeve (300), and the first end abuts the other.
9. The methanol reactor according to claim 7 or 8, characterized in that The support (340) is spiral-shaped, and / or the support (340) is plate-shaped.
10. The methanol reactor of claim 7, wherein, The methanol reactor comprises a temporary fixing member (500), and the temporary fixing member (500) comprises a mounted state and a free state, wherein: In the mounted state, the temporary fixing member (500) is connected with the inner tube (310) and the outer tube (320), and the inner tube (310) and the outer tube (320) are fixed relative to each other along the center line direction of the shell (100); In the free state, the temporary fixing member (500) is separated from the heat exchange sleeve (300).
11. The methanol reactor of claim 10, wherein, The end of the outer tube (320) away from the air inlet (110) is a blocked end, the second end of the inner tube (310) abuts the blocked end, and the support (340) is fixedly connected to the outer wall of the inner tube (310); The temporary fixing member (500) comprises a fixing block (510) and a threaded connecting member (520), the fixing block (510) is provided with a first groove (511) for accommodating part of the wall of the outer tube (320), the groove wall of the first groove (511) is provided with a threaded hole (513) in communication with the space inside the groove, and the threaded connecting member (520) is threadedly connected with the threaded hole (513) to lock or unlock the fixing block (510) and the outer tube (320), the fixing block (510) is provided with a clamping space (512) for accommodating part of the support (340). In the case that the threaded connection (520) locks the fixing block (510) and the outer tube (320), and the partial support (340) is located in the clamping space (512), the support (340) limits the fixing block (510) in the direction from the first end to the second end of the inner tube (310), and the temporary fixing (500) is in the installed state.