A fluidized bed reactor, a hot water removal pipe and its application in acrylonitrile production

Abstract

This invention relates to a fluidized bed reactor and a decooling pipe, and their application in acrylonitrile manufacturing. The fluidized bed reactor includes at least a reaction decooling section and vertical internal components disposed within the reaction decooling section. When transversely cut along a direction perpendicular to the central axis of the fluidized bed reactor, let the cross-sectional area of ​​the reaction decooling section be S1 (in m²), and the outer perimeter of the cross-section of the vertical internal components be L1 (in m), then L1 / S1 = 2.0 - 4.3 m⁻¹. The fluidized bed reactor can promote early bubble breakage and effectively limit bubble growth.

Description

[Technical Field]

[0001] This invention relates to a fluidized bed reactor and a hot water removal pipe, the hot water removal pipe being particularly suitable for installation in the fluidized bed reactor. The invention further relates to the application of the fluidized bed reactor and the hot water removal pipe in acrylonitrile manufacturing. [Previous Technology]

[0002] Acrylonitrile is an important chemical raw material in the petrochemical industry. The one-step ammoxidation process of propylene to produce acrylonitrile is widely used worldwide. This involves the ammoxidation of propylene to acrylonitrile under the action of a fluidized bed catalyst at specific reaction temperatures and pressures, while acetonitrile, hydrogen cyanide, and other byproducts are also produced, along with deep oxidation products such as CO and CO2. This reaction is strongly exothermic, generating a large amount of heat during the process.

[0003] Typical internal components of an acrylonitrile fluidized bed reactor include an propylene-ammonia distributor, an air distribution plate, a deheating water pipe (also known as a cooling coil), and a cyclone separator. The deheating water pipe and the feed legs of the cyclone separator, as vertical components of the fluidized bed, are located within the catalyst bed. The deheating water pipe removes a large amount of generated reaction heat from the reaction system in a timely manner, maintaining the reaction temperature at a stable level. The cyclone separator captures the catalyst entrained during the upward movement of the gas and returns the catalyst to the catalyst bed via the feed legs, thereby reducing catalyst loss.

[0004] The conventional vertical components of a fluidized bed reactor are shown in Figures 1 and 2. Figure 1 is an axial view of the vertical component, and Figure 2 is a cross-sectional view of the vertical component. The vertical component includes a deheating water pipe and a cyclone separator feed leg. The deheating water pipe includes a cooling water pipe and a superheated water pipe. The high-pressure steam generated by the superheated water pipe is usually used as an air compressor and refrigeration turbine. Alternatively, depending on the actual situation of the device, the deheating water pipe may only have a cooling water pipe. Here, the aforementioned deheating water pipe generally includes an inlet, a straight pipe section, and an outlet, with adjacent straight pipe sections fluidly connected by a U-shaped tube.

[0005] Chinese patent applications CN104941532A and CN104941529A disclose a cooling coil design for an ammonia oxidation reactor. The cooling coil can be more tightly encapsulated by providing independent lines that define the cooling coil in a lateral rather than a linear arrangement.

[0006] Chinese patent application CN104624401A discloses an improved cyclone separator configuration. Each multi-stage group of this cyclone separator includes a first-stage cyclone separator having a first-stage inlet, the first-stage cyclone separator being configured to receive an upward-flowing reactor stream from a fluidized catalyst bed in a reactor and to separate at least a portion of the catalyst from the reactor stream. The ratio of the first-stage inlet area to the usable cross-sectional area of ​​the reactor per square meter is approximately 0.03 to approximately 0.05. [Summary of the Invention]

[0007] When using a fluidized bed reactor for the ammoxidation of propylene to produce acrylonitrile, the ammoxidation reaction is a gas-solid heterogeneous catalytic reaction. The gas flow pattern within the reactor differs from that in a free bubbling bed; the bubbles generated by the gas through the distribution plate increase in size as the bed rises. The inventors of this invention have discovered that the presence of vertical internal components helps to break up bubbles. Compared to large bubbles, smaller bubbles are more conducive to mass transfer and increase the formation of effective products. The inventors of this invention have further discovered that, in addition to their basic functions, the hot water pipe and the cyclone separator, as vertical components, also play a role in breaking up bubbles and helping to reduce the degree of backmixing of the gas and solid phases, thus reducing the formation of deep oxidation products. The distribution of these vertical components across the reactor cross-section directly relates to whether bubble growth can be effectively limited or broken up, that is, directly affects the reaction results. This invention is based on this discovery.

[0008] Specifically, the present invention relates to the following: 1. A fluidized bed reactor, comprising at least a reaction decooling section and a vertical internal component disposed within the reaction decooling section, wherein the length of the reaction decooling section along the central axis of the fluidized bed reactor is L (in meters), and within the entire region of the length L of the reaction decooling section, preferably within a region of 49% L above and below the center point of the reaction decooling section (more preferably within a region of 45% L above and 38% L below the center point of the reaction decooling section, and even more preferably within a region of 40% L above and 8% L below the center point of the reaction decooling section), when transversely cut at any position along a direction perpendicular to the central axis of the fluidized bed reactor, let the area of ​​the cross-section of the reaction decooling section be S1 (in meters), and the perimeter of the outer contour of the cross-section of the vertical internal component (when there are multiple cross-sections, it refers to the sum of the outer contour perimeters of all the cross-sections) be L1 (in meters), then L1 / S1 = 2.0 - 4.3 m-1, better L1 / S1=2.2-4.1 m-1, even better L1 / S1=2.4-3.9 m-1.

[0009] 2. The fluidized bed reactor described above or below, wherein the vertical internal components are a combination of hot water pipes or hot water pipes and a gas-solid separation device (preferably a cyclone separator).

[0010] 3. The fluidized bed reactor described above or below, wherein the vertical internal component is a hot water pipe. When transversely cut along a direction perpendicular to the central axis of the fluidized bed reactor, let the area of ​​the cross-section of the reaction decooling section be S1 (in m2), and the perimeter of the outer contour of the cross-section of the hot water pipe (in terms of straight pipe sections) (when there are multiple cross-sections, it refers to the sum of the outer contour perimeters of all the cross-sections) be L2 (in m). Then L2 / S1 = 1.7-3.6 m-1, preferably L2 / S1 = 1.9-3.5 m-1, more preferably L2 / S1 = 2.1-3.3 m-1. The vertical internal component may also include a gas-solid separation device (preferably a cyclone separator). When transversely cut along a direction perpendicular to the central axis of the fluidized bed reactor, let the area of ​​the cross-section of the reaction decooling section be S1. (Unit: m2) The outer perimeter of the cross-section of the above-mentioned gas-solid separation device (measured by the material leg) (when there are multiple cross-sections, it refers to the sum of the outer perimeters of all the above-mentioned cross-sections) is L3 (unit: m), then L3 / S1=0.25-0.85 m-1, preferably L3 / S1=0.30-0.75 m-1, and even more preferably L3 / S1=0.35-0.65 m-1.

[0011] 4. The fluidized bed reactor described above or below, wherein the number of hot water pipes (in terms of straight pipe sections) is 220-5000, preferably 300-2400, and / or the number of gas-solid separation devices (in terms of feed legs) is 16-516, preferably 16-210, and / or the ratio of the number of straight pipe sections to the number of feed legs is 8.5-24.0, preferably 10.0-23.0, and more preferably 11.5-21.0.

[0012] 5. The fluidized bed reactor described in any of the foregoing or subsequent descriptions, wherein the outer diameter of each straight pipe section is the same or different from each other, each independently being 80-180 mm, preferably 90-170 mm, and / or the inner diameter of each straight pipe section is the same or different from each other, each independently being 60-150 mm, preferably 70-140 mm, and / or the length of each straight pipe section is the same or different from each other, each independently being 4.0-13 m, preferably 5.5-12.0 m, and / or the outer diameter of each feed leg is the same or different from each other, each independently being 150-410 mm, preferably 200-360 mm, and / or the inner diameter of each feed leg is the same or different from each other, each independently being 130-400 mm, preferably 180-350 mm, and / or the length of each feed leg is the same or different from each other, each independently being 6-14 m, preferably 10-13 m. m, and / or, the diameter of the above reaction section excluding the cold section is 5-29 m, preferably 7-20 m, the above area S1 is 19.6-660 m2, preferably 38.5-314 m2, and / or, the above length L = 4-12.5 m, preferably 5.5-11.5 m.

[0013] 6. The fluidized bed reactor described above or below includes, from top to bottom, a head, a dilute phase zone, the above-mentioned reaction decooling section, a pre-reaction section and a cone, and also includes a gas distribution plate disposed in the above-mentioned pre-reaction section and a fluid distributor selected as appropriate.

[0014] 7. The fluidized bed reactor described above or below, wherein the cross-section of the reaction cooling section is substantially circular, and / or the inner and outer contours of the cross-section of the vertical internal component are substantially circular, and / or the inner contour of the cross-section of the vertical internal component is substantially circular and the outer contour is substantially circular with protrusions, and / or the vertical internal component includes a heat removal pipe, the heat removal pipe including a heat removal medium inlet, n straight pipe (preferably straight circular pipe) sections and a heat removal medium. The outlet, wherein the first end of the first straight pipe section is connected to the inlet of the heat removal medium, the last end of the nth straight pipe section is connected to the outlet of the heat removal medium, and the last end of the ith straight pipe section is connected to the first end of the (i+1)th straight pipe section by a U-shaped pipe, wherein n is an integer from 2 to 100 (preferably an integer from 2 to 20), i is any integer from 1 to n-1, and has protrusions on the outer wall of some or all (e.g., 1-100%, 5-80%, or 10-40%) of the straight pipe sections.

[0015] 8. A heat removal pipe, comprising a heat removal medium inlet, n straight pipe (preferably straight circular pipe) segments and a heat removal medium outlet, wherein the first end of the first straight pipe segment is connected to the heat removal medium inlet, the last end of the nth straight pipe segment is connected to the heat removal medium outlet, and the last end of the i-th straight pipe segment is connected to the first end of the (i+1)-th straight pipe segment by a U-shaped pipe, wherein n is an integer from 2 to 100 (preferably an integer from 2 to 20), i is any integer from 1 to n-1, and has protrusions on the outer wall of some or all (e.g., 1-100%, 5-80%, or 10-40%) of the straight pipe segments.

[0016] 9. Except for hot water pipes, as described in any of the foregoing or following embodiments, wherein the outer diameter of each straight pipe segment is the same or different from each other, and each is independently 80-180 mm, preferably 90-170 mm, and / or the inner diameter of each straight pipe segment is the same or different from each other, and each is independently 60-150 mm, preferably 70-140 mm, and / or the length of each straight pipe segment is the same or different from each other, and each is independently 4.0-13.0 m, preferably 5.5-12.0 m, and / or the center lines of any two adjacent straight pipe segments are parallel to each other and the distance between the center lines of any two adjacent straight pipe segments is the same or different from each other (preferably the same), and each is independently 160-540 mm, preferably 180-430 mm.

[0017] 10. Except for hot water pipes described above or below, wherein the protrusion extends continuously or discontinuously along the direction of the center line of the straight pipe section, and / or the protrusion extends continuously or discontinuously around the center line of the straight pipe section (e.g., continuously or discontinuously in a ring or spiral shape).

[0018] 11. The hot water pipe described in any of the foregoing or subsequent embodiments, wherein when the protrusion extends continuously or discontinuously along the centerline of the straight pipe section, the extension length Lt of the protrusion is not greater than the length Lz of the straight pipe section (preferably Lt / Lz is 0.05-0.95, more preferably 0.1-0.6), and / or, when the protrusion extends continuously or discontinuously in a ring shape around the centerline of the straight pipe section, the height Hh of the ring is not greater than the length Lz of the straight pipe section (preferably Hh / Lz is 0-0.5, more preferably 0.01-0.3), or, when the protrusion extends continuously or discontinuously in a spiral shape around the centerline of the straight pipe section, the height Ht of the spiral is not greater than the length Lz of the straight pipe section. (Preferably Ht / Lz is 0.1-0.95, more preferably 0.2-0.6), and / or, the height of the protrusion is 0.005-0.3 times (preferably 0.008-0.1 times) the outer diameter of the straight pipe section, and / or, the width of the protrusion is 0.005-0.3 times (preferably 0.008-0.2 times) the outer diameter of the straight pipe section.

[0019] 12. The hot water pipe described above or below, wherein the protrusion extends continuously or discontinuously around the center line of the straight pipe section, and the angle between the center line of the protrusion and the center line of the straight pipe section is greater than 0° and not greater than 90° (preferably not less than 5° and not greater than 75°, more preferably not less than 10° and not greater than 60°).

[0020] 13. A fluidized bed reactor, comprising, from top to bottom, a head, a dilute phase zone, a dense phase zone and a cone, wherein at least one hot water removal pipe as described above or below is provided in the dense phase zone.

[0021] 14. Use of a fluidized bed reactor as described above or below, for the production of epoxides (e.g., propylene oxide) or unsaturated nitriles (e.g., acrylonitrile) by olefin (e.g., propylene) oxidation or ammonia oxidation.

[0022] 15. A method for producing an unsaturated nitrile, comprising the step of subjecting an olefin (e.g., propylene) to an ammoxidation reaction in a fluidized bed reactor as described above or below to generate an unsaturated nitrile (e.g., acrylonitrile).

Implementation Method

[0023] The specific embodiments of the present invention will be described in detail below. However, it should be noted that the scope of protection of the present invention is not limited to these specific embodiments, but is determined by the scope of the patent application in the appendix.

[0024] All publications, patent applications, patents and other references mentioned in this specification are incorporated herein by reference. Unless otherwise defined, all technical and scientific terms used in this specification have the meanings commonly understood by one skilled in the art. In case of conflict, the definitions in this specification shall prevail.

[0025] When this specification uses the prefixes “known to those skilled in the art”, “prior art” or similar terms to derive materials, substances, methods, steps, apparatus or components, the objects derived from such prefixes cover those known and used in the art at the time of the filing of this application, but also include those that are not currently commonly used, but will become generally recognized in the art as suitable for similar purposes.

[0026] In the context of this specification, "substantially" means that deviations that are acceptable or reasonable to a person skilled in the art are permitted, such as deviations within ±10%, ±5%, ±1%, ±0.5%, or ±0.1%.

[0027] Unless otherwise specified, all percentages, parts, ratios, etc. mentioned in this specification are based on weight, and the pressure is gauge pressure.

[0028] In the context of this specification, any two or more embodiments of the present invention may be arbitrarily combined, and the resulting technical solutions are part of the original disclosure of this specification and also fall within the protection scope of the present invention.

[0029] According to one embodiment of the present invention, a fluidized bed reactor, particularly a fluidized bed reactor for acrylonitrile production, is provided. Here, the fluidized bed reactor includes at least a reaction cooling section and vertical internal components disposed within the reaction cooling section.

[0030] According to one embodiment of the present invention, let the length of the reaction decooling section along the central axis of the fluidized bed reactor be L (in meters). Then, when a cross-section is cut at any position along a direction perpendicular to the central axis of the fluidized bed reactor within the entire region of the reaction decooling section of the aforementioned length L, a cross-section of the reaction decooling section and a cross-section of the vertical internal component are obtained on the cross-sectional plane. Moreover, when there are multiple vertical internal components, multiple cross-sections of the vertical internal components are obtained. These cross-sections have an outer contour, which has an area and a perimeter (called the outer contour perimeter), such as the circles represented by 4, 8, and 9 in Figure 3. Here, let the area of ​​the cross-section of the reaction decooling section be S1 (in meters), and the outer contour perimeter of the cross-section of the vertical internal component (when there are multiple cross-sections, it refers to the sum of the outer contour perimeters of all the cross-sections) be L1 (in meters), then L1 / S1 = 2.0 - 4.3 m-1. Here, preferably within a region of 49% L above and below the center point of the aforementioned reaction cooling section, more preferably within a region of 45% L above and 38% L below the center point of the aforementioned reaction cooling section, and even more preferably within a region of 40% L above and 8% L below the center point of the aforementioned reaction cooling section, L1 / S1 = 2.0-4.3 m⁻¹. More preferably, L1 / S1 = 2.2-4.1 m⁻¹, and even more preferably, L1 / S1 = 2.4-3.9 m⁻¹. A L1 / S1 below 2.0 m⁻¹ may cause unstable operation of the device, while a L1 / S1 above 4.3 m⁻¹ may excessively restrict the maintenance space within the reactor. According to one embodiment of the present invention, the aforementioned vertical internal component can specifically be exemplified by a hot water pipe or a gas-solid separation device, particularly a combination of the aforementioned hot water pipe and the aforementioned gas-solid separation device.

[0031] According to one embodiment of the present invention, the cross-sectional area S1 of the above-mentioned reaction cooling section is generally 19.6-660 m2, preferably 38.5-314 m2.

[0032] According to one embodiment of the present invention, when the outer contour is substantially circular, the outer contour circumference = 3.14 × D. Here, D is the diameter of the outer contour (in meters), corresponding to the outer diameter (in meters) of the relevant vertical internal component (such as the straight pipe section excluding the hot water pipe or the material leg of the cyclone separator).

[0033] According to one embodiment of the present invention, the length L of the above-mentioned reaction decooling section along the central axis of the above-mentioned fluidized bed reactor is generally 4-12.5 m, preferably 5.5-11.5 m.

[0034] According to one embodiment of the present invention, the aforementioned hot water pipe includes a cooling water pipe and a superheated water pipe. The function of the cooling water pipe is to use the latent heat of the coolant inside the pipe to carry away the heat generated by the reaction from the reaction system, and the function of the superheated water pipe is to use the sensible heat of the coolant inside the pipe to carry away the heat generated by the reaction from the reaction system. Here, the diameter of the aforementioned cooling water pipe and the aforementioned superheated water pipe can be the same, or they can be different, or they can refer to the dimensions known in the art, without any particular limitation.

[0035] According to one embodiment of the present invention, the straight pipe sections of the aforementioned hot water removal pipes are substantially located in the dense phase region of the aforementioned fluidized bed reactor, for timely removal of reaction heat from the system and maintenance of stable system operation. Therefore, in the context of this specification, the term "reaction decooling section" refers to the area in the aforementioned fluidized bed reactor where hot water removal pipes are provided, and more particularly to the area in the aforementioned fluidized bed reactor where the straight pipe sections of the aforementioned hot water removal pipes are located, and even more particularly to the area in the dense phase region of the aforementioned fluidized bed reactor where the straight pipe sections of the aforementioned hot water removal pipes are provided.

[0036] According to one embodiment of the present invention, the aforementioned hot water removal pipe includes an inlet, a straight pipe section, and an outlet. Adjacent straight pipe sections are generally connected and fluidly communicated by a U-shaped pipe. Here, the aforementioned hot water removal pipe may contain only one straight pipe section, only one U-shaped pipe, or multiple U-shaped pipes connected in series. The larger the number of U-shaped pipes, the larger the outer perimeter L1. Furthermore, the aforementioned hot water removal pipes are typically evenly distributed within the fluidized bed reactor. Specifically, if the fluidized bed reactor is divided into four quadrants (A, B, C, D), the outer perimeter of the aforementioned hot water removal pipes in each quadrant is substantially the same.

[0037] According to one embodiment of the present invention, a cyclone separator is particularly suitable as the above-mentioned gas-solid separation device. Here, the cyclone separator includes a gas inlet, a conical cylinder, an ash hopper, a feed leg, and a gas outlet, wherein the feed leg, as a vertical member, is located within the catalyst bed, i.e., the dense phase region of the fluidized bed reactor, while the other components are located in the dilute phase region of the fluidized bed reactor above the reactor. Here, the cyclone separator can be single-stage or two or more connected in series, with one cyclone separator corresponding to one feed leg. Generally, the feed leg of the first-stage cyclone separator extends to the lower end of the catalyst bed (corresponding to the lower end of the dense phase region), while the feed leg of the second (third)-stage cyclone separator extends to a certain position at the lower, middle, or upper end of the catalyst bed (corresponding to the lower, middle, or upper end of the dense phase region).

[0038] According to one embodiment of the present invention, the above-mentioned cyclone separators are generally arranged in two or more series. During the operation of the fluidized bed reactor, some fine-particle catalyst is separated from the bed with the reaction gas. The catalyst entrained by the gas enters from the inlet of the first-stage cyclone. After passing through the first-stage cyclone, most of the catalyst falls back into the bed along the first-stage cyclone feed leg. A small portion of the catalyst enters the second-stage cyclone with the gas to continue gas-solid separation. The catalyst is then sent back to the catalyst bed along the second-stage cyclone feed leg. The end of the second-stage cyclone feed leg is equipped with a wing valve. The second-stage cyclone can continue to be connected in series with a third-stage cyclone for further gas-solid separation. The catalyst is sent back to the catalyst bed along the feed leg, and the gas leaves the reactor upward through the gas collection chamber. Each cyclone separator has one feed leg for sending the separated catalyst back to the catalyst bed. A set of multi-stage cyclone separators has multiple feed legs.

[0039] According to one embodiment of the present invention, the above-mentioned vertical internal component is the above-mentioned hot water pipe. When it is transversely cut along the direction perpendicular to the central axis of the above-mentioned fluidized bed reactor, let the area of ​​the cross-section of the above-mentioned reaction decooling section be S1 (in m2), and the perimeter of the outer contour of the cross-section of the above-mentioned hot water pipe (in terms of straight pipe section) (when there are multiple above-mentioned cross-sections, it refers to the sum of the perimeters of the outer contour of all the above-mentioned cross-sections) be L2 (in m). Then L2 / S1=1.7-3.6 m-1, more preferably L2 / S1=1.9-3.5 m-1, and more preferably L2 / S1=2.1-3.3 m-1. When the ratio is below 1.7 m-1, it may cause obstacles to the long-term stable operation of the reactor. For example, the heat transfer coefficient may be reduced due to the adhesion of molybdenum sheets on the wall of the hot water pipe, which may cause the temperature control to fail. When the ratio is above 3.6 m-1, it means that the number of hot water pipes increases. Although this is beneficial to the bubble breaking system, it will cause inconvenience for technicians during equipment maintenance.

[0040] According to one embodiment of the present invention, in the above-mentioned fluidized bed reactor, the number of hot water pipes (in terms of straight pipe sections) is generally 220-5000, preferably 300-2400.

[0041] According to one embodiment of the present invention, the outer diameter of each straight pipe section of the hot water pipe is the same or different from each other, and each is independently 80-180 mm, preferably 90-170 mm.

[0042] According to one embodiment of the present invention, the inner diameter of each straight pipe section other than the hot water pipe is the same or different from each other, and each is independently 60-150 mm, preferably 70-140 mm.

[0043] According to one embodiment of the present invention, the lengths of the straight pipe sections other than the hot water pipe are the same or different from each other, and each is independently 4.0-13 m, preferably 5.5-12.0 m.

[0044] According to one embodiment of the present invention, the aforementioned vertical internal component is the aforementioned gas-solid separation device, particularly the aforementioned cyclone separator. Therefore, when transversely cut along a direction perpendicular to the central axis of the fluidized bed reactor, let the area of ​​the cross-section of the reaction cooling section be S1 (in m²), and the perimeter of the outer contour of the cross-section of the gas-solid separation device (measured in terms of the feed leg) (when there are multiple such cross-sections, it refers to the sum of the outer contour perimeters of all such cross-sections) be L3 (in m). Then, L3 / S1 = 0.25-0.85 m⁻¹, preferably L3 / S1 = 0.30-0.75 m⁻¹, and more preferably L3 / S1 = 0.35-0.65 m⁻¹. When this ratio is less than 0.25 m⁻¹, there may be a risk of insufficient catalyst separation or feed leg blockage. Conversely, when the ratio is higher than 0.85 m⁻¹, it will increase equipment costs and occupy more effective space in the reactor. Under the same reaction conditions, the increase in reaction operating line velocity will lead to a further increase in catalyst entrainment.

[0045] According to one embodiment of the present invention, in the above-mentioned fluidized bed reactor, the number of the above-mentioned gas-solid separation devices (in terms of feed legs) is 16-516, preferably 16-210.

[0046] According to one embodiment of the present invention, in the above-mentioned fluidized bed reactor, the ratio of the number of the straight pipe section to the number of the feed leg is 8.5-24.0, preferably 10.0-23.0, and more preferably 11.5-21.0.

[0047] According to one embodiment of the present invention, the outer diameter of each material leg of the gas-solid separation device is the same or different from each other, and each is independently 150-410 mm, preferably 200-360 mm.

[0048] According to one embodiment of the present invention, the inner diameter of each material leg of the gas-solid separation device is the same or different from each other, and each is independently 130-400 mm, preferably 180-350 mm.

[0049] According to one embodiment of the present invention, the lengths of each material leg of the above-mentioned gas-solid separation device are the same or different from each other, and each is independently 6-14 m, preferably 10-13 m.

[0050] According to one embodiment of the present invention, the fluidized bed reactor sequentially includes, from top to bottom, a head, a dilute phase zone, a reaction decooling section, a pre-reaction section, and a cone, and also includes a gas distribution plate disposed in the pre-reaction section and a fluid distributor selected as appropriate. Here, the fluidized bed reactor is preferably a fluidized bed reactor for acrylonitrile manufacturing. In this case, the other distribution plate is an air distribution plate, and the fluid distributor is an propylene-ammonia distributor. Regarding the structure and operation method of the fluidized bed reactor, especially the fluidized bed reactor for acrylonitrile manufacturing, those skilled in the art can directly apply the relevant technical information in this art, and will not be elaborated here.

[0051] According to one embodiment of the present invention, the cross-section of the above-mentioned reaction decooling section is substantially circular. In addition, the diameter of the above-mentioned reaction decooling section is generally 5-29 m, preferably 7-20 m, but is not always limited to this.

[0052] According to one embodiment of the present invention, the inner and outer contours of the cross-section of the above-mentioned vertical inner member are substantially circular. Therefore, the above-mentioned vertical inner member is substantially circular tube-shaped, especially a straight circular tube-shaped.

[0053] According to one embodiment of the present invention, the inner contour of the aforementioned vertical inner member is substantially circular, while the outer contour is substantially circular with protrusions. Therefore, the outer shape of the aforementioned vertical inner member is a substantially circular tube shape with protrusions, and the interior is a substantially circular tube shape. As a vertical inner member with such a specific structure, the hot water removal pipe of the present invention described below is particularly exemplified, a key feature of which is that it has protrusions on the outer wall of a portion or all of the straight pipe section.

[0054] According to one embodiment of the present invention, the aforementioned vertical internal component includes the hot water pipe of the present invention as described below. With respect to this particular structure of the vertical internal component, the outer contour of its cross-section is no longer substantially circular, but rather has a convex substantially circular shape (i.e., an irregular shape). Therefore, it is necessary to calculate the perimeter of the aforementioned outer contour according to the specific characteristics of this irregular shape. However, regardless of the shape of the irregular shape, those skilled in the art can calculate the perimeter of the outer contour of the shape using known mathematical and geometric methods, which will not be elaborated upon here.

[0055] According to one embodiment of the present invention, a heat removal medium pipe is also provided, comprising a heat removal medium inlet, n straight pipe sections, and a heat removal medium outlet. Here, a straight circular pipe is preferred as the aforementioned straight pipe.

[0056] According to one embodiment of the present invention, in the above-mentioned hot water pipe, the first end of the first straight pipe section is connected to the inlet of the heat removal medium, the last end of the nth straight pipe section is connected to the outlet of the heat removal medium, the last end of the i-th straight pipe section is connected to the first end of the (i+1)-th straight pipe section by a U-shaped pipe, and a protrusion is provided on the outer wall of a portion or all of the above-mentioned straight pipe sections. Here, n is an integer from 2 to 100, preferably an integer from 2 to 20. i is any integer from 1 to n-1. In addition, the term "a portion or all" includes, for example, 1-100%, 5-80%, or 10-40% of the total quantity, but is not always limited to these.

[0057] According to one embodiment of the present invention, the protrusion is connected to the outer wall of the straight pipe section. There is no particular limitation on the method of connection; spot welding, continuous welding, integral molding, or other methods are all acceptable.

[0058] According to one embodiment of the present invention, the outer diameter of each straight pipe section of the hot water pipe is the same or different from each other, and each is independently 80-180 mm, preferably 90-170 mm.

[0059] According to one embodiment of the present invention, the inner diameter of each straight pipe section other than the hot water pipe may be the same or different from each other, and each is independently 60-150 mm, preferably 70-140 mm.

[0060] According to one embodiment of the present invention, the lengths of the straight pipe sections other than the hot water pipe are the same or different from each other, and each is independently 4.0-13.0 m, preferably 5.5-12.0 m.

[0061] According to one embodiment of the present invention, in the above-mentioned hot water pipe, the center lines of any two adjacent straight pipe sections are parallel to each other and the distance between the center lines of any two adjacent straight pipe sections is the same or different (preferably the same), and each is independently 160-540 mm, preferably 180-430 mm.

[0062] According to one embodiment of the present invention, in the above-mentioned hot water pipe, the protrusions extend continuously or discontinuously along (parallel to) the center line of the straight pipe section. Here, the number of the protrusions may be 1 to 10, 1 to 4, 1 or 2.

[0063] According to one embodiment of the present invention, in the above-mentioned hot water pipe, the protrusion extends continuously or discontinuously around the center line of the straight pipe section, for example, in a ring or spiral shape. Here, the number of the protrusions can be 1 to 20, 1 to 10, 1 to 4, 1 or 2.

[0064] According to one embodiment of the present invention, in the above-mentioned hot water pipe, when the protrusion extends continuously or discontinuously along the direction of the center line of the straight pipe section, the extension length Lt of the protrusion is not greater than the length Lz of the straight pipe section, preferably Lt / Lz is 0.05-0.95, more preferably 0.1-0.6. When there are multiple protrusions, the different protrusions can be parallel to each other or at an angle to each other, preferably parallel to each other, and more preferably uniformly arranged along the radial direction of the straight pipe section.

[0065] According to one embodiment of the present invention, in the above-mentioned hot water pipe, when the protrusion extends continuously or discontinuously in a ring shape around the center line of the straight pipe section, the height Hh of the ring is not greater than the length Lz of the straight pipe section, preferably Hh / Lz is 0-0.9, more preferably 0.01-0.6. Here, the height Hh refers to the length of the corresponding section of the straight pipe section having the protrusion. When there are multiple protrusions, the vertical interval l1 between different protrusions is not greater than the length Lz of the straight pipe section, preferably l1 / Lz is 0.01-0.5, more preferably 0.03-0.4. Preferably, the angle α1 between the center line of the protrusion and the center line of the straight pipe section is greater than 0° and not greater than 90°, preferably not less than 5° and not greater than 75°, more preferably not less than 10° and not greater than 60°.

[0066] According to one embodiment of the present invention, in the above-mentioned hot water pipe, when the protrusion extends continuously or discontinuously in a spiral form around the center line of the straight pipe section, the height Ht of the spiral is not greater than the length Lz of the straight pipe section, preferably Ht / Lz is 0.1-0.95, more preferably 0.2-0.6. Here, the height Ht refers to the length of the corresponding section of the straight pipe section having the protrusion. In addition, the pitch l1 of the spiral is not greater than the length Lz of the straight pipe section, preferably l1 / Lz is 0.01-0.5, more preferably 0.03-0.4. Preferably, the angle α1 between the center line of the protrusion and the center line of the straight pipe section is greater than 0° and not greater than 90°, preferably not less than 5° and not greater than 75°, more preferably not less than 10° and not greater than 60°. Furthermore, preferably, the angle α2 between the tangent of the aforementioned protrusion along the straight pipe section and the centerline of the aforementioned straight pipe section is not less than 0° and not greater than 90°, more preferably not less than 5° and not greater than 75°, and even more preferably not less than 10° and not greater than 60°.

[0067] According to one embodiment of the present invention, in the above-mentioned non-hot water pipe, the height of the protrusion is 0.005-0.3 times the outer diameter of the straight pipe section, preferably 0.008-0.1 times.

[0068] According to one embodiment of the present invention, in the above-mentioned non-hot water pipe, the width of the protrusion is 0.005-0.3 times the outer diameter of the above-mentioned straight pipe section, preferably 0.008-0.2 times.

[0069] According to one embodiment of the present invention, a fluidized bed reactor is also provided, which sequentially includes a head, a dilute phase region, a dense phase region, and a cone from top to bottom. Here, at least one hot water removal pipe as described in the preceding embodiment of the present invention is provided in the dense phase region. Preferably, the hot water removal pipes are uniformly distributed within the fluidized bed reactor. Specifically, if the fluidized bed reactor is divided into four quadrants (A, B, C, and D), the perimeter of the outline excluding the hot water pipes in each quadrant is substantially the same. Furthermore, the fluidized bed reactor is preferably a fluidized bed reactor for acrylonitrile manufacturing. Regarding the structure and operation method of the fluidized bed reactor, especially the fluidized bed reactor for acrylonitrile manufacturing, those skilled in the art can directly apply the relevant technical information in this art, and will not be elaborated further here.

[0070] According to one embodiment of the present invention, in the above-mentioned fluidized bed reactor, in addition to the hot water removal pipes of the specific structure of the present invention, hot water removal pipes of conventional and known structures in this art can also be provided. Preferably, the number of hot water removal pipes of the specific structure of the present invention accounts for, for example, 1-100%, 5-80%, or 10-40% of the total number of hot water removal pipes, and the number is measured in straight pipe sections. Preferably, these hot water removal pipes are evenly distributed in the above-mentioned fluidized bed reactor. Specifically, if the above-mentioned fluidized bed reactor is divided into four quadrants A, B, C, and D, the perimeter of the outline excluding the hot water pipes in each quadrant is substantially the same.

[0071] According to one embodiment of the present invention, the use of the fluidized bed reactor described in the preceding embodiment in the production of epoxides or unsaturated nitriles by olefin oxidation or ammonia oxidation is also discussed. Here, propylene is particularly used as the olefin, propylene oxide is particularly used as the epoxide, and acrylonitrile is particularly used as the unsaturated nitrile.

[0072] According to one embodiment of the present invention, a method for producing acrylonitrile is particularly relevant, the method comprising the step of subjecting propylene to an ammoxidation reaction in a fluidized bed reactor as described in the preceding embodiment of the present invention to produce acrylonitrile.

[0073] According to one embodiment of the present invention, the above-mentioned olefin oxidation or ammonia oxidation method can be carried out in any manner and method known in the art, such information being known to those skilled in the art and will not be repeated here. Nevertheless, specific operating conditions for the above-mentioned ammonia oxidation reaction include, for example, a molar ratio of propylene / ammonia / air (in terms of molecular oxygen) of generally 1:1.1-1.3:1.8-2.0, a reaction temperature of generally 420-440°C, a reaction pressure (gauge pressure) of generally 0.03-0.14 MPa, and a weight-to-space velocity of generally 0.04-0.10 h⁻¹.

[0074] Examples The present invention will be further described in detail below by way of examples and comparative examples, but the present invention is not limited to the following examples.

[0075] In the following examples and comparative examples, the acrylonitrile yield and propylene conversion rate can be calculated according to the following formulas: Acrylonitrile yield: AN%=CAN / ΣC*100 Propylene conversion rate: Cc3%=(1-Cc3out / Cc3in)*100 Where: CAN: Number of carbon moles (mol) in AN in the reactor outlet gas ΣC: Total number of carbon moles (mol) in the reactor outlet gas Cc3out: Number of carbon moles (mol) in C3 in the reactor outlet gas Cc3out: Number of carbon moles (mol) in C3 in the reactor inlet gas In the following examples and comparative examples, the fluidization of the fluidized bed can also be characterized by pressure pulsation intensity graphs or data.

[0076] Comparative Example 1: The fluidized bed reactor, as shown in Figure 1, has a diameter of 1.5 meters and a tangential height of 16 meters (i.e., the total height of the dense phase and dilute phase regions in the attached figure). It is loaded with 3.8 tons of SANC series acrylonitrile catalyst from the Shanghai Research Institute of Petrochemical Technology, Sinopec. It contains 13 U-shaped tubes (excluding hot water pipes), with the outer diameter of the straight section of the hot water pipe being 30 mm and the length of the straight section being 10 meters. It also contains two sets of cyclone separators connected in series, with the outer diameters of the primary and secondary feed legs being 50 mm and 50 mm, respectively. The length of the primary feed leg is 15.5 meters, and the length of the secondary feed leg is 14.7 meters.

[0077] The diameter of the decooling section of the above-mentioned fluidized bed reactor is 1.5 m, and the length L is 8.5 m. At the center point of the above-mentioned decooling section, L1 / S1=1.74 m-1, L2 / S1=1.39 m-1, and L3 / S1=0.36 m-1.

[0078] Operating conditions of the device: air feed rate is 3200 NM3 / h, temperature is room temperature, and pressure is atmospheric pressure.

[0079] The pressure pulsation intensity data were measured at a distance of 2 meters from H0, as shown in Figure 6.

[0080] Comparative Example 2: The fluidized bed reactor, as shown in Figure 1, has a diameter of 1.5 meters and a tangential height of 16 meters (i.e., the total height of the dense phase and dilute phase regions in the attached figure). It is loaded with 3.8 tons of SANC series acrylonitrile catalyst from the Shanghai Research Institute of Petrochemical Technology, Sinopec. It contains 39 U-shaped pipes (excluding hot water pipes), with the outer diameter of the straight pipe section excluding the hot water pipe being 30 mm and the length of the straight pipe section being 10 meters. It also contains two sets of cyclone separators connected in series in two stages. The outer diameters of the primary and secondary feed legs are 50 mm and 50 mm, respectively. The length of the primary feed leg is 15.5 meters, and the length of the secondary feed leg is 14.7 meters.

[0081] The diameter of the decooling section of the above-mentioned fluidized bed reactor is 1.5 m, and the length L is 8.5 m. At the center point of the above-mentioned decooling section, L1 / S1=4.52 m-1, L2 / S1=4.16 m-1, and L3 / S1=0.36 m-1.

[0082] Operating conditions of the device: air feed rate is 3200 NM3 / h, temperature is room temperature, and pressure is atmospheric pressure.

[0083] The pressure pulsation intensity data were measured at a distance of 2 meters from H0, as shown in Figure 7.

[0084] During the operation of the device, it was found that the concentration of fine catalyst particles in the gas phase at the outlet of the device increased, indicating that the catalyst wear was relatively large.

[0085] Example 1: The fluidized bed reactor, as shown in Figure 1, has a diameter of 1.5 meters and a tangential height of 16 meters (i.e., the total height of the dense phase and dilute phase regions in the attached figure). It is filled with 3.8 tons of SANC series acrylonitrile catalyst from the Shanghai Research Institute of Petrochemical Technology, Sinopec. It contains 30 U-shaped pipes (excluding hot water pipes), with the outer diameter of the straight pipe section excluding the hot water pipe being 30 mm and the length of the straight pipe section being 10 meters. It also contains two sets of cyclone separators, connected in series in two stages. The outer diameters of the primary and secondary feed legs are 50 mm and 50 mm, respectively. The length of the primary feed leg is 15.5 meters, and the length of the secondary feed leg is 14.7 meters.

[0086] The diameter of the decooling section of the above-mentioned fluidized bed reactor is 1.5 m, and the length L is 8.5 m. At the center point of the above-mentioned decooling section, L1 / S1=3.56 m-1, L2 / S1=3.20 m-1, and L3 / S1=0.36 m-1.

[0087] Operating conditions of the device: air feed rate is 3200 NM3 / h, temperature is room temperature, and pressure is atmospheric pressure.

[0088] The pressure pulsation intensity data were measured at a distance of 2 meters from H0, as shown in Figure 8.

[0089] Example 2: The fluidized bed reactor, as shown in Figure 1, has a diameter of 1.5 meters and a tangential height of 16 meters (i.e., the total height of the dense phase and dilute phase regions in the attached figure). It is filled with 3.8 tons of SANC series acrylonitrile catalyst from the Shanghai Research Institute of Petrochemical Technology, Sinopec. It contains 18 U-shaped pipes (excluding hot water pipes), with the outer diameter of the straight pipe section excluding the hot water pipe being 30 mm and the length of the straight pipe section being 10 meters. It also contains two sets of cyclone separators, connected in series in two stages. The outer diameters of the primary and secondary feed legs are 50 mm and 50 mm, respectively. The length of the primary feed leg is 15.5 meters, and the length of the secondary feed leg is 14.7 meters.

[0090] The diameter of the decooling section of the above-mentioned fluidized bed reactor is 1.5 m, and the length L is 8.5 m. At the center point of the above-mentioned decooling section, L1 / S1=2.28 m-1, L2 / S1=1.92 m-1, and L3 / S1=0.36 m-1.

[0091] Operating conditions of the device: air feed rate is 3200 NM3 / h, temperature is room temperature, and pressure is atmospheric pressure.

[0092] The pressure pulsation intensity data were measured at a distance of 2 meters from H0, as shown in Figure 9.

[0093] Example 3: The fluidized bed reactor, as shown in Figure 1, has a diameter of 1.5 meters and a tangential height of 16 meters (i.e., the total height of the dense phase and dilute phase regions in the attached figure). It is filled with 3.8 tons of SANC series acrylonitrile catalyst from the Shanghai Research Institute of Petrochemical Technology, Sinopec. It contains 36 U-shaped pipes (excluding hot water pipes), with the outer diameter of the straight pipe section excluding the hot water pipe being 30 mm and the length of the straight pipe section being 10 meters. It also contains two sets of cyclone separators connected in series in two stages. The outer diameters of the primary and secondary feed legs are 50 mm and 50 mm, respectively. The length of the primary feed leg is 15.5 meters, and the length of the secondary feed leg is 14.7 meters.

[0094] The diameter of the decooling section of the above-mentioned fluidized bed reactor is 1.5 m, and the length L is 8.5 m. At the center point of the above-mentioned decooling section, L1 / S1=4.20 m-1, L2 / S1=3.84 m-1, and L3 / S1=0.36 m-1.

[0095] Operating conditions of the device: air feed rate is 3200 NM3 / h, temperature is room temperature, and pressure is atmospheric pressure.

[0096] The pressure pulsation intensity data were measured at a distance of 2 meters from H0, as shown in Figure 10.

[0097] During the operation of the device, the concentration of fine particulate catalyst in the gas phase at the device outlet is within an acceptable range.

[0098] Comparative Example 3: The fluidized bed reactor, as shown in Figure 1, has a diameter of 8 meters and a tangential height of 18 meters (i.e., the total height of the dense phase and dilute phase regions in the attached figure). It is filled with 160 tons of SANC series acrylonitrile catalyst from the Shanghai Research Institute of Petrochemical Technology, Sinopec. It contains 100 U-shaped hot water pipes, divided into 18 groups. Each group consists of 2, 5, and 6 U-shaped pipes connected in series. The outer diameter of the straight section of the hot water pipe is 114 mm, and the length of the straight section is 8 meters. It also contains 18 cyclone separators in 9 groups, connected in two-stage series. The outer diameters of the primary and secondary feed legs are 326 mm and 219 mm, respectively. The length of the primary feed leg is 12.0 meters, and the length of the secondary feed leg is 10.1 meters.

[0099] The ratio of the number of cooling water pipes to the number of cyclone feed legs in the above-mentioned fluidized bed reactor is 11.11.

[0100] The diameter of the decooling section of the above-mentioned fluidized bed reactor is 8 m, and the length L is 6.9 m. At the center point of the above-mentioned decooling section, L1 / S1=1.73 m-1, L2 / S1=1.43 m-1, and L3 / S1=0.31 m-1.

[0101] The pressure pulsation intensity data was measured at a distance of 2 meters where H0 is. The pressure pulsation intensity data graph is similar to that of Comparative Example 1.

[0102] Unit operating conditions: propylene feed rate is 5900 NM3 / h, reaction temperature is 430℃, reaction pressure is 0.055MPa, propylene:ammonia:air ratio is 1:1.2:9.6.

[0103] Unit operation results: AN yield was 78.3%, and propylene conversion rate was 95.4%.

[0104] Example 4: The fluidized bed reactor, as shown in Figure 4, has a diameter of 8 meters and a tangential height of 18 meters (i.e., the total height of the dense phase and dilute phase regions in the attached figure). It is filled with 160 tons of SANC series acrylonitrile catalyst from the Shanghai Research Institute of Petrochemical Technology, Sinopec. It contains 225 U-shaped hot water pipes, divided into 40 groups. Each group consists of 2, 5, or 6 U-shaped pipes connected in series. The outer diameter of the straight section of the hot water pipe is 114 mm, the length of the straight section is 10 meters, and the pipe spacing is 220 mm. It also contains 11 groups of 20 cyclone separators, connected in two-stage series. The outer diameters of the primary and secondary feed legs are 326 mm and 219 mm, respectively. The length of the primary feed leg is 12.0 meters, and the length of the secondary feed leg is 10.1 meters.

[0105] The ratio of the number of cooling water pipes to the number of cyclone feed legs in the above-mentioned fluidized bed reactor is 20.45.

[0106] The diameter of the decooling section of the above-mentioned fluidized bed reactor is 8 m, and the length L is 7.4 m. At the center point of the above-mentioned decooling section, L1 / S1=3.58 m-1, L2 / S1=3.21 m-1, and L3 / S1=0.37 m-1.

[0107] Pressure pulsation intensity data was measured at a distance of 2 meters where H0 is. The pressure pulsation intensity data graph is similar to that in Example 1.

[0108] Unit operating conditions: propylene feed rate is 5900 NM3 / h, reaction temperature is 430℃, reaction pressure is 0.04 MPa, propylene:ammonia:air ratio is 1:1.2:9.6.

[0109] Unit operation results: AN yield was 80.5%, and propylene conversion rate was 98.5%.

[0110] Example 5: The fluidized bed reactor, as shown in Figure 4, has a diameter of 8 meters and a tangential height of 18 meters (i.e., the total height of the dense and dilute phase regions in the attached figure). It is filled with 160 tons of SANC series acrylonitrile catalyst from the Shanghai Research Institute of Petrochemical Technology, Sinopec. It contains 110 U-shaped hot water pipes, divided into 20 groups. Each group consists of 2, 5, or 6 U-shaped pipes connected in series. The outer diameter of the straight section of the hot water pipe is 114 mm, the length of the straight section is 10 meters, and the pipe spacing is 220 mm. It also contains 14 groups of 28 cyclone separators, connected in two-stage series. The outer diameters of the primary and secondary feed legs are 326 mm and 219 mm, respectively. The length of the primary feed leg is 12.0 meters, and the length of the secondary feed leg is 10.1 meters.

[0111] The ratio of the number of cooling water pipes to the number of cyclone feed legs in the above-mentioned fluidized bed reactor is 7.85.

[0112] The diameter of the decooling section of the above-mentioned fluidized bed reactor is 8 m, and the length L is 7.4 m. At the center point of the above-mentioned decooling section, L1 / S1=2.04 m-1, L2 / S1=1.57 m-1, and L3 / S1=0.48 m-1.

[0113] Pressure pulsation intensity data was measured at a distance of 2 meters where H0 is. The pressure pulsation intensity data graph is similar to that of Example 2.

[0114] Unit operating conditions: propylene feed rate is 5900 NM3 / h, reaction temperature is 430℃, reaction pressure is 0.04 MPa, propylene:ammonia:air ratio is 1:1.2:9.6.

[0115] Unit operation results: AN yield was 79.3%, and propylene conversion rate was 96.8%.

[0116] Example 6: The fluidized bed reactor, as shown in Figure 4, has a diameter of 8 meters and a tangential height of 18 meters (i.e., the total height of the dense and dilute phase regions in the attached figure). It is filled with 160 tons of SANC series acrylonitrile catalyst from the Shanghai Research Institute of Petrochemical Technology, Sinopec. It contains 266 U-shaped hot water pipes, divided into 48 groups. Each group consists of 2, 5, or 6 U-shaped pipes connected in series. The outer diameter of the straight section of the hot water pipe is 114 mm, the length of the straight section is 10 meters, and the pipe spacing is 215 mm. It also contains 18 cyclone separators in 9 groups, connected in two-stage series. The outer diameters of the primary and secondary feed legs are 326 mm and 219 mm, respectively. The length of the primary feed leg is 12.0 meters, and the length of the secondary feed leg is 10.1 meters.

[0117] The ratio of the number of cooling water pipes to the number of cyclone feed legs in the above-mentioned fluidized bed reactor is 29.55.

[0118] The diameter of the decooling section of the above-mentioned fluidized bed reactor is 8 m, and the length L is 7.4 m. At the center point of the above-mentioned decooling section, L1 / S1=4.10 m-1, L2 / S1=3.79 m-1, and L3 / S1=0.31 m-1.

[0119] Pressure pulsation intensity data was measured at a distance of 2 meters where H0 is. The pressure pulsation intensity data graph is similar to that of Example 3.

[0120] Unit operating conditions: propylene feed rate is 5900 NM3 / h, reaction temperature is 430℃, reaction pressure is 0.04 MPa, propylene:ammonia:air ratio is 1:1.2:9.6.

[0121] Unit operation results: AN yield was 80.5%, and propylene conversion rate was 98.6%.

[0122] Example 7: The fluidized bed reactor, as shown in Figure 4, has a diameter of 8 meters and a tangential height of 18 meters (i.e., the total height of the dense and dilute phase regions in the attached figure). It is filled with 160 tons of SANC series acrylonitrile catalyst from the Shanghai Research Institute of Petrochemical Technology, Sinopec. It contains 225 U-shaped hot water pipes, divided into 40 groups. Each group consists of 2, 5, or 6 U-shaped pipes connected in series. The outer diameter of the straight section of the hot water pipe is 114 mm, the length of the straight section is 10 meters, and the pipe spacing is 220 mm. It also contains 12 cyclone separators in 4 groups, connected in three stages in series. The outer diameters of the primary, secondary, and tertiary feed leg pipes are 326 mm, 219 mm, and 219 mm, respectively. The length of the primary feed leg is 12.0 meters, and the lengths of the secondary and tertiary feed legs are 10.1 meters.

[0123] The diameter of the decooling section of the above-mentioned fluidized bed reactor is 8 m, and the length L is 7.4 m. At the center point of the above-mentioned decooling section, L1 / S1=3.40 m-1, L2 / S1=3.21 m-1, and L3 / S1=0.19 m-1.

[0124] Pressure pulsation intensity data was measured at a distance of 2 meters where H0 is. The pressure pulsation intensity data graph is similar to that in Example 1.

[0125] Unit operating conditions: propylene feed rate is 5900 NM3 / h, reaction temperature is 430℃, reaction pressure is 0.04 MPa, propylene:ammonia:air ratio is 1:1.2:9.6.

[0126] Unit operation results: AN yield was 79.5%, and propylene conversion rate was 97.6%.

[0127] Example 8: The fluidized bed reactor, as shown in Figure 4, has a diameter of 8 meters and a tangential height of 18 meters (i.e., the total height of the dense and dilute phase regions in the attached figure). It is filled with 160 tons of SANC series acrylonitrile catalyst from the Shanghai Research Institute of Petrochemical Technology, Sinopec. It contains 225 U-shaped hot water pipes, divided into 40 groups. Each group consists of 2, 5, or 6 U-shaped pipes connected in series. The outer diameter of the straight section of the hot water pipe is 114 mm, the length of the straight section is 10 meters, and the pipe spacing is 220 mm. It also contains 24 cyclone separators in 8 groups, connected in three stages in series. The outer diameters of the primary, secondary, and tertiary feed leg pipes are 326 mm, 219 mm, and 219 mm, respectively. The length of the primary feed leg is 12.0 meters, and the lengths of the secondary and tertiary feed legs are 10.1 meters.

[0128] The diameter of the decooling section of the above-mentioned fluidized bed reactor is 8 m, and the length L is 7.4 m. At the center point of the above-mentioned decooling section, L1 / S1=3.23 m-1, L2 / S1=2.85 m-1, and L3 / S1=0.38 m-1.

[0129] Pressure pulsation intensity data was measured at a distance of 2 meters where H0 is. The pressure pulsation intensity data graph is similar to that in Example 1.

[0130] Unit operating conditions: propylene feed rate is 5900 NM3 / h, reaction temperature is 430℃, reaction pressure is 0.04 MPa, propylene:ammonia:air ratio is 1:1.2:9.6.

[0131] Unit operation results: AN yield was 80.2%, and propylene conversion rate was 98.1%.

[0132] Example 9: The fluidized bed reactor, as shown in Figure 4, has a diameter of 8 meters and a tangential height of 18 meters (i.e., the total height of the dense phase and dilute phase regions in the attached figure). It is filled with 160 tons of SANC series acrylonitrile catalyst from the Shanghai Research Institute of Petrochemical Technology, Sinopec. It contains 140 U-shaped hot water pipes, divided into 26 groups. Each group consists of 2, 5, or 6 U-shaped pipes connected in series. The outer diameter of the straight section of the hot water pipe is 114 mm, and the length of the straight section is 8 meters. It also contains 18 cyclone separators in 9 groups, connected in two-stage series. The outer diameters of the primary and secondary feed legs are 326 mm and 219 mm, respectively. The length of the primary feed leg is 12.0 meters, and the length of the secondary feed leg is 10.1 meters.

[0133] The diameter of the decooling section of the above-mentioned fluidized bed reactor is 8 m, and the length L is 7.2 m. At the center point of the above-mentioned decooling section, L1 / S1=2.28 m-1, L2 / S1=2.00 m-1, and L3 / S1=0.29 m-1.

[0134] Pressure pulsation intensity data was measured at a distance of 2 meters from H0. The pressure pulsation intensity data graph is similar to that of Example 2.

[0135] Unit operating conditions: propylene feed rate is 5900 NM3 / h, reaction temperature is 430℃, reaction pressure is 0.04 MPa, propylene:ammonia:air ratio is 1:1.2:9.6.

[0136] Unit operation results: AN yield was 79.6%, and propylene conversion rate was 97.3%.

[0137] Example 10: The fluidized bed reactor, as shown in Figure 4, has a diameter of 8 meters and a tangential height of 18 meters (i.e., the total height of the dense and dilute phase regions in the attached figure). It is filled with 160 tons of SANC series acrylonitrile catalyst from the Shanghai Research Institute of Petrochemical Technology, Sinopec. It contains 190 U-shaped hot water pipes, divided into 34 groups. Each group consists of 2, 5, or 6 U-shaped pipes connected in series. The outer diameter of the straight pipe section excluding the hot water pipe is 114 mm, and the length (Lz) of the straight pipe section is 8 meters. 95 straight pipe sections have fins on their outer walls, as shown in Figure 5f. Four fins are evenly distributed on the outer pipe wall, with a length (Lt) of 3000 mm, a height of 10 mm, and a width of 20 mm. It also contains 11 groups of 22 cyclone separators, connected in two-stage series. The outer diameters of the primary and secondary feed leg pipes are 326 mm and 219 mm, respectively. The length of the first-stage material leg is 12.0 meters, and the length of the second-stage material leg is 10.1 meters.

[0138] The diameter of the decooling section of the above-mentioned fluidized bed reactor is 8 m, and the length L is 7.4 m. At the center point of the above-mentioned decooling section, L1 / S1=3.12 m-1, L2 / S1=2.75 m-1, and L3 / S1=0.37 m-1.

[0139] Pressure pulsation intensity data was measured at a distance of 2 meters from H0. The pressure pulsation intensity data graph is similar to that of Example 1.

[0140] Unit operating conditions: propylene feed rate is 5900 NM3 / h, reaction temperature is 430℃, reaction pressure is 0.04 MPa, propylene:ammonia:air ratio is 1:1.2:9.6.

[0141] Unit operation results: AN yield was 80.7%, and propylene conversion rate was 98.8%.

[0142] Example 11 The fluidized bed reactor, as shown in Figure 4, has a diameter of 8 meters and a tangential height of 18 meters (i.e., the total height of the dense and dilute phase regions in the attached figure). It is filled with 160 tons of SANC series acrylonitrile catalyst from the Shanghai Research Institute of Petrochemical Technology, Sinopec. It contains 190 U-shaped hot water pipes, divided into 34 groups. Each group consists of 2, 5, or 6 U-shaped pipes connected in series. The outer diameter of the straight pipe section excluding the hot water pipe is 114 mm, and the length (Lz) of the straight pipe section is 8 meters. 95 straight pipe sections have fins on their outer walls, as shown in Figure 5a. Eight fins are distributed on the outer pipe wall, with a vertical spacing of 500 mm between the fins and an angle α1 of 50°. The fins have a length (Lt) of 3500 mm, a height of 10 mm, and a width of 20 mm. It also contains 10 groups of 20 cyclone separators, connected in two-stage series. The outer diameters of the primary and secondary feed leg pipes are 326 mm and 219 mm, respectively. The length of the first-stage material leg is 12.0 meters, and the length of the second-stage material leg is 10.1 meters.

[0143] The diameter of the decooling section of the above-mentioned fluidized bed reactor is 8 m, and the length L is 7.4 m. At the center point of the above-mentioned decooling section, L1 / S1=3.15 m-1, L2 / S1=2.78 m-1, and L3 / S1=0.37 m-1.

[0144] Pressure pulsation intensity data was measured at a distance of 2 meters from H0. The pressure pulsation intensity data graph is similar to that of Example 1.

[0145] Unit operating conditions: propylene feed rate is 5900 NM3 / h, reaction temperature is 430℃, reaction pressure is 0.04 MPa, propylene:ammonia:air ratio is 1:1.2:9.6.

[0146] Unit operation results: AN yield was 80.6%, and propylene conversion rate was 98.7%.

[0147] Example 12: The fluidized bed reactor, as shown in Figure 4, has a diameter of 8 meters and a tangential height of 18 meters (i.e., the total height of the dense phase and dilute phase regions in the attached figure). It is filled with 160 tons of SANC series acrylonitrile catalyst from the Shanghai Research Institute of Petrochemical Technology, Sinopec. It contains 225 U-shaped hot water pipes, divided into 40 groups. Each group consists of 2, 5, or 6 U-shaped pipes connected in series. The outer diameter of the straight section of the hot water pipe is 114 mm, and the length of the straight section is 8 meters. It also contains 21 groups of 42 cyclone separators, connected in two-stage series. The outer diameters of the primary and secondary feed legs are 400 mm and 325 mm, respectively. The length of the primary feed leg is 12.0 meters, and the length of the secondary feed leg is 10.1 meters.

[0148] The diameter of the decooling section of the above-mentioned fluidized bed reactor is 8 m, and the length L is 7.2 m. At the center point of the above-mentioned decooling section, L1 / S1=4.16 m-1, L2 / S1=3.21 m-1, and L3 / S1=0.95 m-1.

[0149] Pressure pulsation intensity data was measured at H0, which is 2 meters. The pressure pulsation intensity data graph is similar to that of Example 1.

[0150] Unit operating conditions: propylene feed rate is 5900 NM3 / h, reaction temperature is 430℃, reaction pressure is 0.04 MPa, propylene:ammonia:air ratio is 1:1.2:9.6.

[0151] Unit operation results: AN yield was 80.1%, and propylene conversion rate was 98.7%. [Simplified Explanation of the Diagram]

[0153] Figure 1 is a front view of a prior art fluidized bed reactor. Figure 2 is a cross-sectional view of the decooling section of a prior art fluidized bed reactor. Figure 3 is a cross-sectional view of the decooling section of the fluidized bed reactor of the present invention. Figure 4 is a front view of the fluidized bed reactor of the present invention. Figure 5 is a schematic diagram of an exemplary embodiment of the hot water pipe of the present invention. Figure 6 is a pressure pulsation intensity graph of Comparative Example 1. Figure 7 is a pressure pulsation intensity graph of Comparative Example 2. Figure 8 is a pressure pulsation intensity graph of Example 1. Figure 9 is a pressure pulsation intensity graph of Example 2. Figure 10 is a pressure pulsation intensity graph of Example 3. Explanation of reference numerals in the attached drawings: 1: Fluidized bed reactor; 2: Raw material mixed gas inlet pipeline; 3: Cyclone separator inlet; 4: Hot water removal pipe; 5: Cyclone separator cylinder; 6: Cyclone separator cone; 7: Cyclone separator ash hopper; 8: Second (third) stage feed leg of the cyclone separator; 9: First stage feed leg of the cyclone separator. Technical effects: According to the fluidized bed reactor of the present invention, the change of flow pattern within the fluidized bed can be promoted as early as possible, promoting bubble breakage. According to the fluidized bed reactor of the present invention, bubble growth can be effectively limited, thereby achieving the purpose of improving the raw material gas conversion rate and increasing the yield of the target reaction product. According to the fluidized bed reactor of the present invention, the degree of backmixing of the gas and solid phases can be reduced, reducing the generation of deep oxidation products. According to the fluidized bed reactor of the present invention, heat and mass transfer efficiency can be improved, and the operating cycle of the device can be extended.

Claims

1. A fluidized bed reactor, comprising at least a reaction decooling section and vertical internal components disposed within the reaction decooling section, wherein the length of the reaction decooling section along the central axis of the fluidized bed reactor is L (in meters), and the area of ​​the cross-section of the reaction decooling section at any position in the region 45% L above and 38% L below the center point of the reaction decooling section is S1 (in meters), and the perimeter of the outer contour of the cross-section of the vertical internal component, when multiple cross-sections exist, refers to the sum of the perimeters of the outer contours of all the cross-sections, which is L1 (in meters), then L1 / S1 = 2.0-4.3 m⁻¹, the vertical internal component is a hot water pipe or a combination of a hot water pipe and a gas-solid separation device, the number of the hot water pipes, in terms of straight pipe sections, is 220-5000, and the number of the gas-solid separation devices, in terms of material legs, is 16-516, and the number of the straight water pipes is... The ratio of the number of pipe segments to the number of the aforementioned material legs is 8.5-24.

0. The aforementioned vertical internal components exclude hot water pipes. The perimeter of the outer contour of the cross-section of the aforementioned vertical internal components, excluding hot water pipes, is calculated based on straight pipe segments. When there are multiple such cross-sections, the perimeter refers to the sum of the outer contour perimeters of all such cross-sections, which is L2, in meters. Therefore, L2 / S1 = 1.7-3.6 m-1. The aforementioned vertical internal components may also include gas-solid separation devices, depending on the situation. The perimeter of the outer contour of the cross-section of the aforementioned gas-solid separation devices, calculated based on material legs, is calculated based on the sum of the outer contour perimeters of all such cross-sections, which is L3, in meters. Therefore, L3 / S1 = 0.25-0.85 m-1.

2. The fluidized bed reactor as requested in item 1, wherein L1 / S1 = 2.2-4.1 m-1.

3. The fluidized bed reactor as requested in item 1, wherein L1 / S1 = 2.4-3.9 m-1.

4. The fluidized bed reactor as requested in item 1, wherein L2 / S1 = 1.9-3.5 m-1, and / or, L3 / S1 = 0.30-0.75 m-1.

5. The fluidized bed reactor as requested in item 1, wherein L2 / S1 = 2.1-3.3 m⁻¹, and / or L3 / S1 = 0.35-0.65 m⁻¹.

6. The fluidized bed reactor of claim 1, wherein the number of the above-mentioned hot water pipes, in terms of straight pipe sections, is 300-2400, and / or the number of the above-mentioned gas-solid separation devices, in terms of material legs, is 16-210, and / or the ratio of the number of the above-mentioned straight pipe sections to the number of the above-mentioned material legs is 11.5-21.

0.

7. The fluidized bed reactor of claim 1, wherein the outer diameter of each straight pipe section is the same or different from each other, and each is independently 80-180 mm, and / or the inner diameter of each straight pipe section is the same or different from each other, and each is independently 60-150 mm, and / or the length of each straight pipe section is the same or different from each other, and each is independently 4.0-13 m, and / or the outer diameter of each feed leg is the same or different from each other, and each is independently 150-410 mm, and / or the inner diameter of each feed leg is the same or different from each other, and each is independently 130-400 mm, and / or the length of each feed leg is the same or different from each other, and each is independently 6-14 m, and / or the diameter of the above-mentioned reactor except the cooling section is 5-29 m, the above-mentioned area S1 is 19.6-660 m2, and / or the above-mentioned length L=4-12.5 m.

8. The fluidized bed reactor of claim 7, wherein the outer diameter of each straight pipe section is the same or different from each other, and each is independently 90-170 mm, and / or the inner diameter of each straight pipe section is the same or different from each other, and each is independently 70-140 mm, and / or the length of each straight pipe section is the same or different from each other, and each is independently 5.5-12.0 m, and / or the outer diameter of each feed leg is the same or different from each other, and each is independently 200-360 mm, and / or the inner diameter of each feed leg is the same or different from each other, and each is independently 180-350 mm, and / or the length of each feed leg is the same or different from each other, and each is independently 10-13 m, and / or the diameter of the above-mentioned reaction except the cooling section is 7-20 m, the above-mentioned area S1 is 38.5-314 m2, and / or the above-mentioned length L=5.5-11.5 m.

9. The fluidized bed reactor of claim 1, which, from top to bottom, includes a head, a dilute phase zone, the aforementioned reaction decooling section, a pre-reaction section, and a cone, and also includes a gas distribution plate disposed in the aforementioned pre-reaction section and a fluid distributor selected as appropriate.

10. The fluidized bed reactor of claim 1, wherein the cross-section of the decooling section is substantially circular, and / or the inner and outer contours of the cross-section of the vertical internal component are substantially circular, and / or the inner contour of the cross-section of the vertical internal component is substantially circular and the outer contour is substantially circular with a protrusion, and / or the vertical internal component includes a deheating water pipe, the deheating water pipe including a deheating medium inlet, n straight pipe sections and a deheating medium outlet, wherein the first end of the first straight pipe section is connected to the deheating medium inlet, the last end of the nth straight pipe section is connected to the deheating medium outlet, the last end of the i-th straight pipe section is connected to the first end of the i+1-th straight pipe section by a U-shaped pipe, wherein n is an integer from 2 to 100, i is any integer from 1 to n-1, and a protrusion is present on the outer wall of some or all of the straight pipe sections.

11. The fluidized bed reactor of claim 10, wherein the straight tube is a straight circular tube, and / or, n is an integer from 2 to 20, and / or, 10-40% of the outer wall of the straight tube section has protrusions.

12. The fluidized bed reactor of claim 10, wherein the centerlines of any two adjacent straight pipe sections are parallel to each other and the distance between the centerlines of any two adjacent straight pipe sections is the same or different, and is independently 160-540 mm.

13. The fluidized bed reactor of claim 12, wherein the centerlines of any two adjacent straight pipe sections are parallel to each other and the distance between the centerlines of any two adjacent straight pipe sections is the same, each being 180-430 mm independently.

14. The fluidized bed reactor of claim 10, wherein the protrusion extends continuously or discontinuously along the direction of the centerline of the straight pipe section, and / or the protrusion extends continuously or discontinuously around the centerline of the straight pipe section.

15. The fluidized bed reactor of claim 14, wherein the aforementioned protrusion extends continuously or discontinuously in an annular or spiral form around the centerline of the aforementioned straight pipe section.

16. The fluidized bed reactor of claim 10, wherein when the protrusion extends continuously or discontinuously along the direction of the centerline of the straight pipe section, the extension length Lt of the protrusion is not greater than the length Lz of the straight pipe section, and / or, when the protrusion extends continuously or discontinuously in a ring shape around the centerline of the straight pipe section, the height Hh of the ring is not greater than the length Lz of the straight pipe section; or, when the protrusion extends continuously or discontinuously in a spiral shape around the centerline of the straight pipe section, the height Ht of the spiral is not greater than the length Lz of the straight pipe section, and / or, the height of the protrusion is 0.005-0.3 times the outer diameter of the straight pipe section, and / or, the width of the protrusion is 0.005-0.3 times the outer diameter of the straight pipe section.

17. The fluidized bed reactor of claim 16, wherein when the protrusion extends continuously or discontinuously along the direction of the centerline of the straight pipe section, Lt / Lz is 0.1-0.6, and / or Hh / Lz is 0.01-0.3, and / or Ht / Lz is 0.2-0.6, and / or the height of the protrusion is 0.008-0.1 times the outer diameter of the straight pipe section, and / or the width of the protrusion is 0.008-0.2 times the outer diameter of the straight pipe section.

18. The fluidized bed reactor of claim 10, wherein the protrusion extends continuously or discontinuously around the centerline of the straight pipe section, and the angle between the centerline of the protrusion and the centerline of the straight pipe section is greater than 0° and not greater than 90°.

19. The fluidized bed reactor of claim 18, wherein the angle between the centerline of the aforementioned protrusion and the centerline of the aforementioned straight pipe section is not less than 10° and not greater than 60°.

20. Use of the fluidized bed reactor as claimed in claim 1 for the production of epoxides or unsaturated nitriles by olefin oxidation or ammonia oxidation.

21. A method for producing an unsaturated nitrile, comprising the step of subjecting an olefin to an ammoxidation reaction in a fluidized bed reactor as claimed in claim 1 to generate an unsaturated nitrile.

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