EA046737B1 - FLUIDIFIED BED REACTOR, HEAT CONDUCTING WATER PIPELINE AND THEIR APPLICATION IN ACRYLONITRILE PRODUCTION - Google Patents

Description

Field of the present invention

The invention relates to a fluidized bed reactor and to a heat removal plumbing which is particularly suitable for placement in a fluidized bed reactor. Furthermore, the present invention relates to the use of a fluidized bed reactor and a heat sink pipe in the production of acrylonitrile.

BACKGROUND OF THE INVENTION

Acrylonitrile is an important chemical feedstock in the petrochemical industry. A one-step process for the production of acrylonitrile by ammoxidation of propylene is widely used throughout the world, in which, under the action of a fluidized bed ammoxidation catalyst and under certain conditions of reaction temperature and pressure, propylene is ammoxidized to produce acrylonitrile along with by-products such as acetonitrile, hydrocyanic acid and others, as well as CO and CO2, which are deep oxidation products. This reaction is highly exothermic and produces a large amount of heat.

A typical fluidized bed reactor for acrylonitrile production contains a propylene and ammonia distributor, an air distribution plate, a heat sink (also known as a cooling coil), and a cyclone separator, with the heat sink and cyclone separator riser located in the catalytic bed as the vertical components of the fluidized bed. The heat sink can remove a large amount of heat that is generated by the reaction from the reaction system over time and maintain the reaction temperature at a steady state, and the cyclone separator can capture the catalyst carried away by the gas that moves upward and return the catalyst to the catalyst bed through the drain riser, resulting in reduced catalyst losses.

Conventional vertical fluidized bed reactor components are shown in FIG. 1 and 2. In FIG. 1 illustrates an axial view of the vertical components, and FIG. 2 illustrates a cross-sectional view of the arrangement of the vertical components. The vertical components are heat removal water pipes and cyclone separator drain risers. Heat-sinking water lines contain a cooling water line and a superheating water line, and the high-pressure steam produced by the superheating water line typically finds application in air compressor turbines and refrigerators. Alternatively, the heat sink plumbing may contain only the cooling plumbing, depending on the actual conditions of the unit. Here, the heat sink pipe generally includes an inlet, a straight pipe section and an outlet, and two adjacent straight pipe sections are in communication to carry fluid through the U-shaped pipe.

PRC patent applications CN104941532A and CN104941529A disclose the design of a cooling coil for an ammoxidation reactor. The cooling coil may be more densely packaged by providing individual piping that defines the cooling coil in a transverse configuration rather than a linear configuration.

PRC patent application CN104624401A discloses an improved configuration of cyclone separators. Each multi-stage cyclone separator system includes a first-stage cyclone separator comprising a first-stage inlet configured to receive an upwardly flowing stream from a reactor fluidized catalyst bed in the reactor and recover at least a portion of the catalyst contained in the reactor stream. The ratio of the first stage inlet area expressed in square meters to the available cross-sectional area of the reactor expressed in square meters is from about 0.03 to about 0.05.

Brief Disclosure of the Invention

When a fluidized bed reactor is used in the ammoxidation reaction of propylene to produce acrylonitrile, the propylene ammoxidation reaction is a heterogeneous catalytic reaction involving gas and solid phases, the flow state of the gas in the reactor being different from that of the free fluidized bed, and the bubbles that are formed during the passage gas through the distribution plate become larger as the layer rises. The present inventors have discovered that the presence of vertical internal components promotes bubble breakdown, and that small bubbles have higher mass transfer conductivity than large bubbles and are thus beneficial for increasing production of usable products. In addition, the present inventors have discovered that heat sinks and cyclone separators acting as vertical components perform a bubble breaking function in addition to their primary functions and can also contribute to reducing gas-solid backmixing and reducing formation of deep oxidation products. The distribution of said vertical components across the cross-section of the reactor has a direct impact on the possible achievement of effective bubble growth limitation or effective bubble destruction and thus has a direct impact on the reaction results. On

- 1 046737 the present invention was made based on the discovery of this fact.

In particular, the present invention relates to the following aspects:

1. A fluidized bed reactor comprising at least a reaction cooling section and a vertical internal component present in the reaction cooling section, wherein the length of the reaction cooling section in a direction along the central axis of the fluidized bed reactor is designated as L (expressed in units m), and, in a cross section running perpendicular to the central axis of the fluidized bed reactor, at an arbitrary position within the region of the entire length L of the reaction cooling section, preferably within the region from 49% L above to 49% L below the central point of the reaction cooling section (preferably within the region from 45% L above to 38% L below the center point of the reaction cooling section, and even more preferably within the region from 40% L above to 8% L below the center point of the reaction cooling section), the area of the transverse cross-section of the reaction cooling section is designated as S1 (expressed in units of ^m2 ), and the outer circumference of the cross-section of the vertical internal component (when there are multiple cross-sections, this means the sum of the outer circumferences of all cross-sections) is designated as L1 (expressed in units of m) , L1/S1 = 2.04.3 m ^-1 , preferably L1/S1 = 2.2-4.1 m ¹ and ^- preferably L1/S1 = 2.4-3.9 m ^-1 .

2. A fluidized bed reactor according to any one of the preceding or subsequent aspects, wherein the vertical internal component is a heat sink conduit or a combination of a heat sink conduit and a gas-solid separator (preferably a cyclone separator).

3. A fluidized bed reactor according to any one of the preceding or subsequent aspects, wherein the vertical internal component is a heat sink conduit, wherein, in a cross section extending perpendicular to the central axis of the fluidized bed reactor, the cross-sectional area of the reaction cooling section is designated as S1 (expressed in units of ^m2 ), and the circumference of the outer contour of the cross-section of the heat sink water pipe (in terms of a straight pipe section) (when there are many cross sections, this means the sum of the outer contour circumferences of all cross sections) is designated as L2 (expressed in units of m ), L2/S1 = 1.7-3.6 m ^-1 , preferably L2/S1 = 1.9-3.5 m ^-1 and more preferably L2/S1 = 2.1-3.3 m ^-1 , and the vertical internal component optionally further comprises a gas-solid separator (preferably a cyclone separator), wherein in a cross-section extending perpendicular to the central axis of the fluidized bed reactor, the cross-sectional area of the reaction cooling section is designated S1 (expressed in units of m ² ), and the outer circumference of the cross-section of the gas-solid separator (in terms of the riser) (when there are multiple cross-sections, this means the sum of the outer circumferences of all cross-sections) is designated as L3 (expressed in units of m), 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 .

4. A fluidized bed reactor according to any one of the preceding or subsequent aspects, wherein the number of heat removal water lines (based on straight pipe section) is 220-5000, preferably 300-2400, and/or the number of gas-solid separators (based on riser) is 16-516 and preferably 16-210, and/or the ratio of the number of straight pipe sections to the number of risers is 8.5-24.0, preferably 10.023.0 and more preferably 11.5-21.0.

5. A fluidized bed reactor according to any one of the preceding or subsequent aspects, wherein the outer diameters of the straight pipe sections, which are the same or different from each other, are in each case independently from 80 to 180 mm, preferably from 90 to 170 mm, and /or the internal diameters of the straight pipe sections, which are the same or different from each other, in each case independently range from 60 to 150 mm and preferably from 70 to 140 mm, and/or the lengths of the straight pipe sections, which are the same or different from each other each other, in each case independently from 4.0 to 13 m and preferably from 5.5 to 12.0 m, and/or the outer diameters of the drain risers, which are the same or different from each other, in each case independently from 150 up to 410 mm and preferably from 200 to 360 mm, and/or the internal diameters of the drain risers, which are the same or different from each other, in each case independently range from 130 to 400 mm and preferably from 180 to 350 mm, and/or lengths the risers, which are the same or different from each other, are in each case independently from 6 to 14 m and preferably from 10 to 13 m, and/or the reaction cooling section has a diameter from 5 to 29 and preferably from 7 to 20 m , the area S1 is from 19.6 to 660 m ² , preferably from 38.5 to 314 m ² , and/or the length L is from 4 to 12.5 m and preferably from 5.5 to 11.5 m.

6. A fluidized bed reactor according to any one of the preceding or subsequent aspects, comprising a head section, a dilute phase zone, a reaction cooling section, a pre-reaction section, and a cone in order from top to bottom, and optionally

- 2 046737 contains a gas distribution plate and optionally a fluid distributor present in the preliminary reaction section.

7. A fluidized bed reactor according to any one of the preceding or subsequent aspects, wherein the reaction cooling section has a substantially circular cross-section, and/or the cross-section of a vertical internal component has a substantially circular inner contour and a substantially circular outer contour, and/or the cross-section of a vertical the internal component has a substantially circular inner contour and a substantially circular outer contour comprising one or more projections, and/or the vertical internal component comprises a heat sink conduit, the heat sink conduit having a heat sink medium inlet, n straight conduit (preferably straight round conduit) sections, and a heat sink medium outlet , wherein the head end of the first straight pipeline section is in communication with the inlet of the heat-removing medium, the tail end of the n-th straight pipeline section is in communication with the outlet of the heat-removing medium, the tail end of the i-th straight pipeline section is in communication with the head end (ί+1 )-ίί straight pipe section through the U-shaped pipe, wherein n is an integer from 2 to 100 (preferably an integer from 2 to 20), i is an arbitrary integer between 1 and n-1, and one or multiple projections on the outer wall of some or all (including 1-100%, 5-80% or 10-40%) of straight pipe sections.

8. A heat-removing pipeline containing an inlet of a heat-removing medium, n straight pipeline (preferably straight round pipeline) sections and an outlet of a heat-removing medium, in which the head end of the first straight pipeline section is in communication with the inlet of the heat-removing medium, the tail end of the n-th straight pipeline section is in communication with the outlet of the heat removal medium, the tail end of the i-th straight pipe section is in communication with the head end of the (ί+1)-ίί straight pipe section through the U-shaped pipe, n is an integer from 2 to 100 (preferably an integer 2 to 20), i is an arbitrary integer between 1 and n-1, and one or more projections are present on the outer wall of some or all (including 1-100%, 5-80% or 10-40%) straight pipeline sections.

9. A heat sink plumbing system according to any one of the preceding or subsequent aspects, wherein the outer diameters of the straight pipe sections, which are the same or different from each other, are in each case independently 80-180 mm and preferably 90-170 mm, and/or inner diameters straight pipe sections that are the same or different from each other, in each case independently 60-150 mm and preferably 70-140 mm, and/or lengths of straight pipe sections that are the same or different from each other, in each case independently are 4.0-13.0 m and preferably 5.5-12.0 m, and/or the center lines of any two adjacent straight pipe sections are parallel to each other and the distances between the center lines of any two adjacent straight pipe sections are the same or different from each other (preferably the same in relation to each other), and in each case they are independently 160-540 mm and preferably 180-430 mm.

10. A heat sink according to any of the preceding or subsequent aspects, wherein one or more projections extend in a continuous or intermittent manner in a direction along the center line of the straight conduit section, and/or one or more protrusions extend in a continuous or intermittent manner around the center line of the straight conduit section (for example, in the shape of a ring or spiral).

11. A heat sink according to any one of the preceding or subsequent aspects, wherein when one or more protrusions extend in a continuous or discontinuous manner in a direction along the center line of the straight pipe section, the length Lt of the one or more protrusions extends no more than the length Lz of the straight pipe section ( preferably Lt/Lz is from 0.05 to 0.95 and more preferably from 0.1 to 0.6), and/or when one or more projections extend in a continuous or discontinuous manner around the center line of the straight ring-shaped pipeline section, the height Hh ring is no more than the length Lz of the straight pipe section (preferably Hh/Lz is from 0 to 0.5 and more preferably from 0.01 to 0.3), or when one or more projections extend in a continuous or discontinuous manner around the center line of the straight pipe section sections in the form of a spiral, the height Ht of the spiral is not more than the length Lz of the straight pipeline section (preferably Ht/Lz is from 0.1 to 0.95 and more preferably from 0.2 to 0.6), and/or the height of one or more of the projections is from 0.005 times to 0.3 times (preferably from 0.008 times to 0.1 times) the outer diameter of the straight pipeline section, and/or the width of one or more projections is from 0.005 times to 0.3 times (preferably from 0.008 -fold to 0.2 times) the outer diameter of the straight pipeline section.

12. A heat sink according to any of the preceding or subsequent aspects, wherein one or more projections extend in a continuous or intermittent manner around the prices

- 3 046737 trawl line of the straight pipeline section, and there is an angle between the center line of one or more projections and the center line of the straight pipeline section that is more than 0° and not more than 90° (preferably not less than 5° and not more than 75 ° and preferably no less than 10° and no more than 60°).

13. A fluidized bed reactor comprising a head section, a dilute phase zone, a dense phase zone, and a cone in order from top to bottom, wherein the dense phase zone contains at least one heat sink according to any of the preceding or following aspects.

14. Use of a fluidized bed reactor according to any of the preceding or subsequent aspects in the production of an epoxy compound (such as propylene oxide) or an unsaturated nitrile (such as acrylonitrile) from an olefin (such as propylene) by an oxidation method or an ammoxidation method.

15. A method for producing unsaturated nitrile, comprising the step of introducing an olefin (such as propylene) into an ammoxidation reaction in a fluidized bed reactor according to any of the preceding or subsequent aspects to produce an unsaturated nitrile (such as acrylonitrile).

Brief description of the figures

In fig. 1 is a schematic front view of a prior art fluidized bed reactor.

In fig. 2 is a schematic cross-sectional view of a reaction cooling section of a prior art fluidized bed reactor.

In fig. 3 is a schematic cross-sectional view of a reaction cooling section of a fluidized bed reactor according to the present invention.

In fig. 4 is a schematic front view of a fluidized bed reactor according to the present invention.

In fig. 5 is a schematic diagram of a heat sink pipe according to an exemplary embodiment of the present invention.

In fig. Figure 6 shows a graph of the intensity of pressure pulsations in comparative example 1.

In fig. Figure 7 shows a graph of the intensity of pressure pulsations in comparative example 2.

In fig. Figure 8 shows a graph of the intensity of pressure pulsations in example 1.

In fig. Figure 9 shows a graph of the intensity of pressure pulsations in example 2.

In fig. Figure 10 shows a graph of the intensity of pressure pulsations in example 3.

List of symbols

- Fluidized bed reactor;

- Supply pipeline for mixed source gas;

- Cyclone separator inlet;

- Heat-dissipating water supply;

- Cyclone separator cylinder;

- Cyclone separator cone;

- Ash ladle of the cyclone separator;

- Drain riser of the second stage (third stage) cyclone separator;

- Drain riser of the first stage cyclone separator.

Technical effects

By using the fluidized bed reactor according to the present invention, the change in the flow pattern in the fluidized bed can be accelerated as quickly as possible, and the destruction of bubbles can be accelerated.

By using the fluidized bed reactor according to the present invention, the growth of bubbles can be effectively limited, so that the conversion rate of the feed gas can be increased, and the yield of the target reaction product can be increased.

By using the fluidized bed reactor according to the present invention, the backmixing of the gas phase and the solid phase and the formation of deep oxidation products can be reduced.

By using the fluidized bed reactor according to the present invention, the efficiency of heat and mass transfer can be improved, and the operating life of the device can be extended.

Detailed Disclosure of the Invention

The invention will be illustrated in detail hereinafter with reference to corresponding embodiments, but it should be noted that the scope of the present invention is not limited to these embodiments, but is defined by the appended claims.

All publications, patent applications, patents and other documents cited herein

- 4 046737 document, are incorporated herein by reference in their entirety. Unless otherwise defined, all technical and scientific terms used herein have the meanings commonly understood by those skilled in the art. In the event of a conflict, the contents of the description herein, including definitions, govern.

When materials, methods, components, devices or systems that are described herein are defined by terms known to those skilled in the art, generally known in the art or similar terms, it should be understood that the aforementioned materials, methods, components, devices or systems are not only those which are traditionally in use in the art at the time of filing this application, but also those which are not generally in use at the present time but will become generally known in the art as being suitable for a similar purpose.

In the context of the present invention, the term practically means that tolerance is a deviation that is acceptable or considered reasonable by those skilled in the art, such as a deviation within ±10%, within ±5%, within ±1%, within ±0 .5% or within ±0.1%.

In the context of the present invention, unless specifically stated otherwise, all percentages, parts, ratios and other quantities are expressed as mass, and all pressures presented are gauge pressure.

In the context of the present invention, any two or more embodiments of the present invention can be optionally combined, and the resulting technical solution forms part of the original disclosure of the present invention and is within the scope of the present invention.

According to an embodiment, the present invention relates to a fluidized bed reactor, in particular to a fluidized bed reactor for the production of acrylonitrile. In this case, the fluidized bed reactor contains at least a reaction cooling section and a vertical internal component located in the reaction cooling section.

According to an embodiment of the present invention, when the length of the reaction cooling section in the direction along the central axis of the fluidized bed reactor is designated as L (expressed in units of m), the cross section of the reaction cooling section and the cross section of the vertical internal component can be obtained in a cross-sectional plane that extends perpendicular to the central axis of the fluidized bed reactor at an arbitrary position within the region of the entire length L of the reaction cooling section. In addition, when a plurality of vertical internal components are present, cross sections of the plurality of vertical internal components can be obtained. Said cross-sections have an outer contour with an area and a circumference (referred to as the outer contour circle), such as the circles represented by numbers 4, 8 and 9 in FIG. 3. Meanwhile, when the cross-sectional area of the reaction cooling section is designated as S1 (expressed in units of m ² ), and the outer circumference of the cross-section of the vertical internal component (when there are multiple cross-sections, this means the sum of the outer circumference of all cross-sections) is designated as L1 (expressed in units of m), L1/S1 = 2.0-4.3 m ^-1 . Here it turns out to be preferable that L1/S1 = 2.0-4.3 m ^-1 within the region from 49% L above to 49% L below the center point of the reaction cooling section, more preferably within the region from 45% L above to 38 %L below the center point of the reaction cooling section and even more preferably within the range of 40% L above to 8% L below the center point of the reaction cooling section. Preferably L1/S1 = 2.2-4.1 m ^-1 and more preferably L1/S1 = 2.4-3.9 m ^-1 . When L1/S1 is less than 2.0 m ^-1 , unstable operation of the device may occur, and when L1/S1 is more than 4.3 m ^-1 , excessively large maintenance space in the reactor may be occupied. According to an embodiment of the present invention, specific examples of the vertical internal component include a heat sink and a gas-solid separator, and in particular, a combination of a heat sink and a gas-solid separator.

According to an embodiment of the present invention, the cross-sectional area S1 of the reaction cooling section is generally from 19.6 to 660 m ² and preferably from 38.5 to 314 m ² .

According to an embodiment of the present invention, when the outer contour is substantially circular in shape, the circumference of the outer contour is 3.14-D, wherein D is the diameter (expressed in units of m) of the outer contour to which the outer diameter (expressed in units of m) corresponds ) a suitable vertical internal component (for example, such as a straight pipe section of a heat sink or a cyclone separator riser).

According to an embodiment of the present invention, the length L of the reaction cooling section in the direction of the central axis of the fluidized bed reactor is generally 4 to 12.5 m and preferably 5.5 to 11.5 m.

- 5 046737

According to an embodiment of the present invention, the heat removal conduit includes a cooling conduit for removing heat that is generated during the reaction process from the reaction system by applying the latent heat of phase change of the cooling medium in the conduit, and a superheating conduit for removing the heat that is generated during the reaction process from the reaction system. by applying the dry heat of the cooling medium in the pipeline. Here, the diameters of the cooling water pipe and the superheating water pipe may be the same or different, and they may be pipes that are conventionally used in engineering without any particular limitation.

According to an embodiment of the present invention, the straight pipe section of the heat removal water line is substantially located in the dense phase region of the fluidized bed reactor and is used to timely remove reaction heat from the system and maintain stable operation of the system. For this purpose, in the context of the description of the present invention, the term reaction cooling section means the region of the fluidized bed reactor in which the heat sink line is located, more particularly the region in the fluidized bed reactor in which the straight piping section of the heat sink water line is located, even more particularly the region in the dense zone fluidized bed reactor phase in which the straight piping section of the heat sink water supply is located.

According to an embodiment of the present invention, the heat sink pipe includes an inlet, a straight pipe section and an outlet, and two adjacent straight pipe sections are generally connected through a U-shaped pipe and are in fluid communication with each other. The heat sink pipe may contain only one straight pipe section, may contain only one U-shaped pipe, or may be formed by connecting a plurality of U-shaped pipes in series. The greater the number of U-shaped pipes, the larger the circumference of the outer contour L1. In addition, heat removal water lines are typically evenly distributed within the fluidized bed reactor. As a specific example, if the fluidized bed reactor is divided into four quadrants ABCD, the outer circumferences of the heat sink pipes in all quadrants are substantially the same.

According to an embodiment of the present invention, the cyclone separator may be referred to as a gas-solid separator. Here, the cyclone separator has a gas inlet, a cone, an ash ladle, a riser and a gas outlet, wherein the riser is present as a vertical component in the catalytic layer being the dense phase zone of the fluidized bed reactor, and other components are located in the dilute phase zone at the top. parts of a fluidized bed reactor. Here, the cyclone separator may be a single-stage cyclone separator, or two or more cyclone separators may be connected in series, and one cyclone separator includes one corresponding downcomer. Typically, the downpipe of the first stage cyclone separator extends to a certain position at the bottom of the catalytic bed (corresponding to the bottom of the dense phase zone), and the downpipe of the second stage (third stage) cyclone separator extends to a certain position at the bottom, middle part or top part of the catalytic layer (corresponding to the lower part, middle part or upper part of the dense phase zone).

According to an embodiment of the present invention, cyclone separators are typically arranged such that two or more cyclone separators are connected in series. During the operation of the fluidized bed reactor, some fine catalyst particles are carried away from the catalytic bed by the reaction gas, the catalyst particles entrained by the gas enter the cyclone separator through the inlet of the first stage cyclone separator, after passing through the first stage cyclone separator, most of the catalyst particles return to the catalytic bed through the outlet riser of the first stage cyclone separator, the remaining few catalyst particles enter the second stage cyclone separator along with gas to further separate the gas and solid phases, the separated catalyst particles return to the catalytic layer through the drain riser of the second stage cyclone separator, while the tail end of the riser of the cyclone separator The second stage separator contains a butterfly valve, the second stage cyclone separator can then be in series connection with the third stage cyclone separator to achieve additional separation of the gas and solid phases, the separated catalyst particles return to the catalytic bed through the downcomer, and the gas moves upward through the gas collection chamber and then leaves the reactor. Each cyclone separator contains a riser to return the separated catalyst to the catalytic bed. Many multi-stage cyclone separators have multiple drain risers.

According to an embodiment of the present invention, the vertical internal component is a heat sink conduit, and wherein, in a cross-section extending perpendicular to the central axis of the fluidized bed reactor, the cross-sectional area of the reaction cooling section is designated S1 (expressed in units of m ² ), and circle

- 6 046737 of the outer contour of the cross section of the heat sink water pipe (in terms of a straight pipeline section) (when there are many cross sections, this means the sum of the circumferences of the outer contour of all cross sections) is designated as L2 (expressed in units of m), L2/S1 = 1, 7-3.6 m ^-1 , preferably L2/S1 = 1.9-3.5 m ^-1 and more preferably L2/S1 = 2.1-3.3 m ^-1 . When the ratio is less than 1.7 m ^-1 , problems may occur during long-term stable operation of the reactor, for example, the heat transfer coefficient may decrease due to the adhesion of molybdenum sheets to the walls of the heat sink pipe, and temperature control may be impaired, and when the ratio is more than 3.6 m ^-1 , this means that the number of heat sink pipes increases, which may be an advantage for breaking bubbles, but will cause inconvenience to technicians when servicing the device.

According to an embodiment of the present invention, the number of heat sink pipes (per straight pipe section) in a fluidized bed reactor is typically 220-5000 and preferably 300-2400.

According to an embodiment of the present invention, the outer diameters of the straight pipe sections of the heat sink water pipe, which are the same or different from each other, are in each case independently 80-180 mm and preferably 90-170 mm.

According to an embodiment of the present invention, the inner diameters of the straight pipe sections of the heat sink water pipe, which are the same or different from each other, are in each case independently 60-150 mm and preferably 70-140 mm.

According to an embodiment of the present invention, the lengths of the straight pipe sections of the heat sink water pipe, which are the same or different from each other, are in each case independently 4.0-13 m and preferably 5.5-12.0 m.

According to an embodiment of the present invention, the vertical internal component is a gas-solid separator, in particular a cyclone separator. For this purpose, in a cross section running perpendicular to the central axis of the fluidized bed reactor, the cross-sectional area of the reaction cooling section is designated as S1 (expressed in units of m ² ), and the outer circumference of the cross-section of the gas-solid separator ( in terms of the drain riser) (when there are many cross sections, this means the sum of the outer contour circumferences of all cross sections) is designated as L3 (expressed in units of m), L3/S1 = 0.25-0.85 m ^-1 , preferably L3 /S1 = 0.30-0.75 m ^-1 and 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 blocking of the downcomer. On the contrary, when this ratio is more than 0.85 m ^-1 , on the one hand, the cost of the equipment will increase, on the other hand, more efficient space in the reactor will be occupied, and under the same reaction conditions the linear operating speed of the reactor will increase, which may cause an additional increase in catalyst carryover.

According to an embodiment of the present invention, the number of gas-solid separators (in terms of riser) in the fluidized bed reactor is from 16 to 516, and preferably from 16 to 210.

According to an embodiment of the present invention, in a fluidized bed reactor, the ratio of the number of straight pipe sections and the number of downcomers is 8.5 to 24.0, preferably 10.0 to 23.0, and more preferably 11.5 to 21.0.

According to an embodiment of the present invention, the outer diameters of the gas-solid separator risers, which are the same or different from each other, are in each case independently 150-410 mm and preferably 200-360 mm.

According to an embodiment of the present invention, the internal diameters of the gas-solid separator risers, which are the same or different from each other, are in each case independently 130-400 mm and preferably 180-350 mm.

According to an embodiment of the present invention, the lengths of the gas-solid separator risers, which are the same or different from each other, are in each case independently from 6 to 14 m and preferably from 10 to 13 m.

According to an embodiment of the present invention, the fluidized bed reactor comprises a head section, a dilute phase zone, a reaction cooling section, a pre-reaction section and a cone in order from top to bottom, and further comprises a gas distribution plate and optionally a fluid distributor present in the pre-reaction section. Here, a fluidized bed reactor for producing acrylonitrile may preferably be referred to as a fluidized bed reactor. In this case, the above-mentioned other distribution plate is an air distribution plate, and the fluid distributor is a propylene and ammonia distributor. To construct and operate a fluidized bed reactor, in particular a fluidized bed reactor for the production of acrylonitrile, etc., relevant technical information known in the art can be directly used by those skilled in the art.

- 7 046737 field of technology, and the corresponding detailed description is not contained in this document.

According to an embodiment of the present invention, the cross-section of the reaction cooling section is substantially circular in shape. In addition, the diameter of the reaction cooling section is typically from 5 to 29 m and preferably from 7 to 20 m, but in some cases is not limited to these values.

According to an embodiment of the present invention, the inner and outer cross-sectional contours of the vertical inner component are substantially circular in shape. For this purpose, the vertical internal component has the shape of a substantially circular pipe and, in particular, a straight circular pipe.

According to an embodiment of the present invention, the vertical inner component has a substantially circular inner contour and a substantially circular outer contour including one or more projections. For this purpose, the exterior of the vertical inner component is a substantially circular pipe containing one or more projections, and the interior of the vertical inner component is a substantially circular pipe. As a vertical internal component of such a structure, mention may be made in particular of the heat sink pipe according to the present invention, which is described later herein, and which is characterized in that there is a projection on the outer wall of some or all of the straight pipe section.

According to an embodiment of the present invention, the vertical internal component includes a heat sink pipe according to the present invention, which is described later herein. With regard to the vertical internal component having such a specific structure, the outer contour of its cross section is no longer substantially circular in shape, but has a substantially circular shape with one or more projections, which is a profiled shape. For this reason, the circumference of the outer contour must be calculated according to the practical position of the profiled shape. However, regardless of what the profiled shape is, those skilled in the art can calculate the circumference of the outer contour of the above-mentioned shape using known mathematical geometry methods, and there is no corresponding detailed description herein.

According to an embodiment of the present invention, there is provided a heat sink pipe, which includes a heat sink medium inlet, n straight pipe sections, and a heat sink medium outlet. Here, the straight round pipe may be preferably referred to as a straight pipe.

According to an embodiment of the present invention, in a heat-removing water pipeline, the head end of the first straight pipeline section is in communication with the inlet of the heat-removing medium, the tail end of the n-th straight pipeline section is in communication with the outlet of the heat-removal medium, the tail end of the i-th straight pipeline section is in communication with the head end of the (|+1)th straight pipe section through the U-shaped pipe, and some or all of the outer walls of the straight pipe sections contain projections. Here, n is an integer from 2 to 100 and preferably 2 to 20, and i is an arbitrary integer between 1 and n-1. In addition, the term some or all means, for example, from 1 to 100%, from 5 to 80%, or from 10 to 40% of the total amount, but in some cases is not limited to these values.

According to an embodiment of the present invention, one or more projections are connected to the outer wall of the straight pipe section. Here, the joining method is not particularly limited, and spot welding, continuous welding, integral molding or other methods may be used.

According to an embodiment of the present invention, the outer diameters of the straight pipe sections of the heat sink water pipe, which are the same or different from each other, are in each case independently 80-180 mm and preferably 90-170 mm.

According to an embodiment of the present invention, the inner diameters of the straight pipe sections of the heat sink water pipe, which are the same or different from each other, are in each case independently 60-150 mm and preferably 70-140 mm.

According to an embodiment of the present invention, the lengths of the straight pipe sections of the heat sink water pipe, which are the same or different from each other, are in each case independently from 4.0 to 13.0 m and preferably from 5.5 to 12.0 m.

According to an embodiment of the present invention, in a heat sink water pipe, the central pipes of any two adjacent straight pipe sections are parallel with respect to each other, and the distances between the central pipes of any two adjacent straight pipe sections are the same or different (preferably the same with respect to each other), and in each case they are independently 160-540 mm and preferably 180-430 mm.

According to an embodiment of the present invention, in a heat sink pipe, one or more projections extend in a continuous or discontinuous manner along (parallel) directions

- 8 046737 lining the central line of a straight pipeline section. Here, the number of one or more projections can be from 1 to 10, from 1 to 4, 1 or 2.

According to an embodiment of the present invention, in a heat sink pipe, one or more projections extend in a continuous or discontinuous manner around the center line of a straight pipe section, for example, in the shape of a ring or a spiral. Here, the number of one or more projections can be from 1 to 20, from 1 to 10, from 1 to 4, 1 or 2.

According to an embodiment of the present invention, in a heat sink water pipe, when one or more protrusions extend in a continuous or discontinuous manner in a direction along the center line of the straight pipe section, the extension length Lt of the protrusion is no more than the length Lz of the straight pipe section, and the ratio Lt/Lz is preferably 0.05-0.95 and preferably 0.1-0.6. In the case of a plurality of projections, the various projections may extend parallel to each other or at an angle to each other, preferably parallel to each other, and are preferably evenly spaced in the radial direction of the above-mentioned straight pipe section.

According to an embodiment of the present invention, in a heat sink water pipe where one or more projections extend in a continuous or discontinuous manner around the center line of the straight pipe section in the form of a ring, the height Hh of the ring is not more than the length Lz of the straight pipe section, Hh/Lz is preferably from 0 to 0.9 and preferably from 0.01 to 0.6. Here, the height Hh means the length of the corresponding section of the straight pipe section having one or more projections. In the case of the presence of a plurality of one or more projections, the vertical distance l1 between the different projections is no more than the length Lz of the straight pipe section, l1/Lz is preferably 0.01-0.5 and more preferably 0.03-0.4. The angle α1 between the center line of one or more protrusions and the center line of the straight pipe section is preferably more than 0° and not more than 90°, more preferably not less than 5° and not more than 75° and even more preferably not less than 10° and not more than 60°.

According to an embodiment of the present invention, in a heat sink water pipe, when one or more projections extend in a continuous or discontinuous manner around the center line of the straight pipe section in the shape of a spiral, the height Ht of the spiral is not more than the length Lz of the straight pipe section, Ht/Lz is preferably 0.1 -0.95 and preferably 0.2-0.6. Here, the height Ht means the length of the corresponding section of the straight pipe section having one or more projections. In addition, the pitch of the spiral screw l1 is not more than the length Lz of the straight pipe section, l1/Lz is preferably 0.01-0.5 and more preferably 0.03-0.4. The angle α1 between the center line of one or more protrusions and the center line of the straight pipe section is preferably more than 0° and not more than 90°, more preferably not less than 5° and not more than 75° and even more preferably not less than 10° and not more than 60°. In addition, the angle α2 between the tangent line of one or more projections along the straight pipeline section and the center line of the straight pipeline section is preferably not less than 0° and not more than 90°, more preferably not less than 5° and not more than 75° and further preferably no less than 10° and no more than 60°.

According to an embodiment of the present invention, in a heat sink water pipe, the height of one or more projections is 0.005 times to 0.3 times, and preferably 0.008 times to 0.1 times, the outer diameter of the straight pipe section.

According to an embodiment of the present invention, in a heat sink water pipe, the width of the one or more projections is 0.005 times to 0.3 times, and preferably 0.008 times to 0.2 times, the outer diameter of the straight pipe section.

According to an embodiment of the present invention, it also relates to a fluidized bed reactor, which contains a head section, a dilute phase zone, a dense phase zone and a cone in order from top to bottom. Here, at least one heat sink according to any of the preceding aspects of the present invention is located in the dense phase zone. Preferably, the heat sink pipes are evenly distributed in the fluidized bed reactor. As a specific example, if the fluidized bed reactor is divided into four quadrants ABCD, the outer circumferences of the heat sink pipes in all quadrants are substantially the same. Moreover, a fluidized bed reactor for producing acrylonitrile may preferably be referred to as a fluidized bed reactor. To construct and operate a fluidized bed reactor, in particular a fluidized bed reactor for producing acrylonitrile, etc., relevant technical information known in the art can be directly used by those skilled in the art, and corresponding detailed description is not available in this document.

According to an embodiment of the present invention, in a fluidized bed reactor, a heat sink pipe having a conventional design that is known in the art may be present in addition to a heat sink pipe having a specific design.

- 9 046737 manual according to the present invention. Preferably, the number of heat sink pipes having a particular design according to the present invention is, for example, 1-100%, 5-80% or 10-40% with respect to the total number of all heat sink pipes, based on a straight pipe section. Preferably, the heat sink pipes are evenly distributed in the fluidized bed reactor. For example, if a fluidized bed reactor is divided into four quadrants ABCD, the outer circumferences of the heat sink pipes in all quadrants are essentially the same.

According to an embodiment of the present invention, it also relates to the use of a fluidized bed reactor according to any of the above aspects of the present invention in the production of an epoxy compound or an unsaturated nitrile using an olefin by an oxidation method or an ammoxidation method. Here, as the olefin, mention may be made in particular of propylene; as epoxide, mention may be made in particular of propylene oxide; and as the unsaturated nitrile, acrylonitrile may be mentioned in particular.

According to an embodiment of the present invention, it relates in particular to a process for producing acrylonitrile, which includes the step of introducing propylene into an ammoxidation reaction in a fluidized bed reactor according to any of the above aspects of the present invention to produce acrylonitrile.

According to an embodiment of the present invention, the process for oxidizing or ammoxidizing olefins can be carried out in any manner and in any mode that is conventionally known in the art, and since such information is known to those skilled in the art, corresponding detailed description is not presented herein. However, in specific examples, the ammoxidation reaction is carried out under the following conditions: the molar ratio of propylene, ammonia and air (in terms of molecular oxygen) is, as a rule, 1:1.1-1.3:1.8-2.0, reaction temperature is generally 420-440°C, the reaction pressure (gauge pressure) is generally 0.03-0.14 MPa, and the hourly feed rate is generally 0.04-0.10 h ^-1 .

Examples

The present invention will now be described in further detail and with reference to examples and comparative examples, but the present invention is not limited to the following examples.

In the following examples and comparative examples, the acrylonitrile yield and propylene conversion can be calculated using the following equations:

Acrylonitrile yield: AN% = CAN/ΣΟ 100;

Propylene conversion degree: C _C3 % = (1-CC _3in /CC _3out )^100, with:

CAN is the molar amount (mol) of carbon contained in acrylonitrile in the gas composition at the outlet of the reactor;

ΣC is the total molar amount (mol) of carbon contained in the gas at the reactor outlet;

CC3out is the molar amount (mol) of carbon contained in propylene in the gas composition at the reactor outlet;

CC3in is the molar amount (mol) of carbon contained in propylene in the reactor inlet gas.

In the following examples and comparative examples, the fluidized state of the fluidized bed can also be characterized by a pressure pulsation intensity graph or related data.

Comparative example 1

As illustrated in FIG. 1, in the fluidized bed reactor, the diameter was 1.5 m, the tangential height was 16 m (i.e., the total height of the dense phase zone and the dilute phase zone, which are illustrated in Fig. 1), the filling was 3.8 tons of catalyst SANC series acrylonitrile synthesis supplied by Shanghai Petrochemical Technology Research Institute SINOPEC, and there were 13 U-shaped heat sink water pipes inside, and the outer diameter of the straight pipe section of each heat sink pipe was 30 mm, and the length of the straight pipe section was 10 m; There were two sets of cyclone separators, and inside each of them there were two stages of cyclone separators connected in series, and the outer diameters of the first stage and second stage risers were 50 mm and 50 mm, respectively, the length of the first stage riser was 15.5 m , and the length of the second stage riser was 14.7 m.

In the reaction cooling section of the fluidized bed reactor, the diameter was 1.5 m and the length L was 8.5 m. At the center point of the reaction cooling section, L1/S1 = 1.74 m ^-1 , L2/S1 = 1.39 m ^{- 1} and L3/S1 = 0.36 m ^-1 .

The device was operated under the following conditions: air supply speed composition

- 10 046737 was 3200 Nm ³ /h, the temperature was room temperature, and the pressure was atmospheric pressure.

The pressure pulsation intensity data were measured at H ₀ = 2 m and are illustrated in Fig. 6.

Comparative example 2

As illustrated in FIG. 1, in the fluidized bed reactor, the diameter was 1.5 m, the tangential height was 16 m (i.e., the total height of the dense phase zone and the dilute phase zone, which are illustrated in Fig. 1), the filling was 3.8 tons of catalyst SANC series acrylonitrile synthesis supplied by Shanghai Petrochemical Technology Research Institute SINOPEC, and there were 39 U-shaped heat sink water pipes inside, and the outer diameter of the straight pipe section of each heat sink pipe was 30 mm, and the length of the straight pipe section was 10 m; there were two sets of cyclone separators, and within each of them there were stages of cyclone separators connected in series, and the outer diameters of the first stage and second stage risers were 50 mm and 50 mm, respectively, the length of the first stage riser was 15.5 m, and the length of the second stage riser was 14.7 m.

In the reaction cooling section of the fluidized bed reactor, the diameter was 1.5 m and the length L was 8.5 m. At the center point of the reaction cooling section, L1/S1 = 4.52 m ^-1 , L2/S1 = 4.16 m ^{- 1} and L3/S1 = 0.36 m ^-1 .

The device was operated under the following conditions: the air flow rate was 3200 Nm ³ /h, the temperature was room temperature, and the pressure was atmospheric pressure.

The pressure pulsation intensity data were measured at H0 = 2 m and are illustrated in Fig. 7.

During operation of the device, it was discovered that the concentration of fine catalyst particles in the gas phase at the outlet of the device increased, which indicated relatively serious abrasive wear of the catalyst.

Example 1

As illustrated in FIG. 1, in the fluidized bed reactor, the diameter was 1.5 m, the tangential height was 16 m (i.e., the total height of the dense phase zone and the dilute phase zone, which are illustrated in Fig. 1), the filling was 3.8 tons of catalyst synthesizing SANC series acrylonitrile supplied by Shanghai Petrochemical Technology Research Institute SINOPEC, and there were 30 U-shaped heat sink water pipes inside, and the outer diameter of the straight pipe section of each heat sink pipe was 30 mm, and the length of the straight pipe section was 10 m; there were two sets of cyclone separators, and within each of them there were stages of cyclone separators connected in series, and the outer diameters of the first stage and second stage risers were 50 mm and 50 mm, respectively, the length of the first stage riser was 15.5 m, and the length of the second stage riser was 14.7 m.

In the reaction cooling section of the fluidized bed reactor, the diameter was 1.5 m and the length L was 8.5 m. At the center point of the reaction cooling section, L1/S1 = 3.56 m ^-1 , L2/S1 = 3.20 m ^{- 1} and L3/S1 = 0.36 m ^-1 .

The device was operated under the following conditions: the air flow rate was 3200 Nm ³ /h, the temperature was room temperature, and the pressure was atmospheric pressure.

The pressure pulsation intensity data were measured at H0 = 2 m and are illustrated in Fig. 8.

Example 2

As illustrated in FIG. 1, in the fluidized bed reactor, the diameter was 1.5 m, the tangential height was 16 m (i.e., the total height of the dense phase zone and the dilute phase zone, which are illustrated in Fig. 1), the filling was 3.8 tons of catalyst synthesizing SANC series acrylonitrile supplied by Shanghai Petrochemical Technology Research Institute SINOPEC, and there were 18 U-shaped heat sink water pipes, and the outer diameter of the straight pipe section of each heat sink pipe was 30 mm, and the length of the straight pipe section was 10 m; there were two sets of cyclone separators, and within each of them there were stages of cyclone separators connected in series, and the outer diameters of the first stage and second stage risers were 50 mm and 50 mm, respectively, the length of the first stage riser was 15.5 m, and the length of the second stage riser was 14.7 m.

In the reaction cooling section of the fluidized bed reactor, the diameter was 1.5 m and the length L was 8.5 m. At the center point of the reaction cooling section, L1/S1 = 2.28 m ^-1 , L2/S1 = 1.92 m ^{- 1} and L3/S1 = 0.36 m ^-1 .

The device was operated under the following conditions: the air flow rate was 3200 Nm ³ /h, the temperature was room temperature, and the pressure was atmospheric pressure.

- 11 046737

The pressure pulsation intensity data were measured at H0 = 2 m and are illustrated in Fig. 9.

Example 3

As illustrated in FIG. 1, in the fluidized bed reactor, the diameter was 1.5 m, the tangential height was 16 m (i.e., the total height of the dense phase zone and the dilute phase zone, which are illustrated in Fig. 1), the filling was 3.8 tons of catalyst synthesizing SANC series acrylonitrile supplied by Shanghai Petrochemical Technology Research Institute SINOPEC, and there were 36 U-shaped heat sink water pipes, and the outer diameter of the straight pipe section of each heat sink pipe was 30 mm, and the length of the straight pipe section was 10 m; there were two sets of cyclone separators, and within each of them there were stages of cyclone separators connected in series, and the outer diameters of the first stage and second stage risers were 50 mm and 50 mm, respectively, the length of the first stage riser was 15.5 m, and the length of the second stage riser was 14.7 m.

In the reaction cooling section of the fluidized bed reactor, the diameter was 1.5 m and the length L was 8.5 m. At the center point of the reaction cooling section, L1/S1 = 4.20 m ^-1 , L2/S1 = 3.84 m ^{- 1} and L3/S1 = 0.36 m ^-1 .

The device was operated under the following conditions: the air flow rate was 3200 Nm ³ /h, the temperature was room temperature, and the pressure was atmospheric pressure.

The pressure pulsation intensity data were measured at H ₀ = 2 m and are illustrated in Fig. 10.

During operation of the device, the concentration of fine catalyst particles in the gas phase at the outlet of the device was within an acceptable range.

Comparative example 3

As illustrated in FIG. 1, in the fluidized bed reactor, the diameter was 8 m, the tangential height was 18 m (i.e., the total height of the dense phase zone and the dilute phase zone, which are illustrated in Fig. 1), the filling was 160 tons of SANC series acrylonitrile synthesis catalyst , which is supplied by Shanghai Petrochemical Technology Research Institute SINOPEC, and inside there were 100 U-shaped heat sink water pipes, which were divided into 18 groups, and each group was formed by connecting two U-shaped, five U-shaped and six U-shaped heat-removing water pipes arranged in series, with the outer diameter of the straight pipeline section of each heat-removing water pipe being 114 mm, and the length of the straight pipeline section being 8 m; and inside there were 18 cyclone separators, which were divided into 9 sets, each of them containing two stages of cyclone separators connected in series, and the outer diameters of the first stage and second stage risers were 326 mm and 219 mm, respectively, the length of the riser the first stage was 12.0 m, and the length of the second stage riser was 10.1 m.

The ratio of the number of cooling water pipes to the number of cyclone separator drain risers in the fluidized bed reactor was 11.11.

In the reaction cooling section of the fluidized bed reactor, the diameter was 8 m and the length L was 6.9 m. At the center point of the reaction cooling section, L1/S1 = 1.73 m- ¹ , L2/S1 = 1.43 m ^-1 and L3/S1 = 0.31 m ^-1 .

The pressure pulsation intensity data was measured at H0 = 2 m, and the graph of the pressure pulsation intensity data was similar to that of Comparative Example 1.

The device was operated under the following conditions: the propylene injection rate was 5900 Nm ³ /h, the reaction temperature was 430°C, the reaction pressure was 0.055 MPa, and the propylene-ammonia-air ratio was 1:1.2:9.6.

As a result of operating the device, the following data were obtained: the yield of acrylonitrile was 78.3%, and the degree of propylene conversion was 95.4%.

Example 4

As illustrated in FIG. 4, in the fluidized bed reactor, the diameter was 8 m, the tangential height was 18 m (i.e., the total height of the dense phase zone and the dilute phase zone, which are illustrated in Fig. 1), the filling was 160 tons of SANC series acrylonitrile synthesis catalyst , which is supplied by Shanghai Petrochemical Technology Research Institute SINOPEC, and inside there were 225 U-shaped heat sink water pipes, which were divided into 40 groups, and each group was formed by connecting two U-shaped, five U-shaped and six U-shaped heat-removing water pipes arranged in series, with the outer diameter of the straight pipeline section of each heat-removing water pipe being 114 mm, the length of the straight pipeline section being 10 m, and the gap between the pipes being 220 mm; and inside there were 20 cyclone separators, which were divided into 11 sets, each of which contained two cyclone stages

- 12 046737 separators connected in series, with the outer diameters of the first stage and second stage risers being 326 mm and 219 mm, respectively, the length of the first stage riser being 12.0 m, and the length of the second stage riser being 10.1 m .

The ratio of the number of cooling water pipes to the number of cyclone separator drain risers in the fluidized bed reactor was 20.45.

In the reaction cooling section of the fluidized bed reactor, the diameter was 8 m and the length L was 7.4 m. At the center point of the reaction cooling section, L1/S1 = 3.58 m ^-1 , L2/S1 = 3.21 m ^-1 and L3/S1 = 0.37 m ^-1 .

The pressure pulsation intensity data was measured at H0 = 2 m, and the graph of the pressure pulsation intensity data was similar to that of Example 1.

The device was operated under the following conditions: the propylene injection rate was 5900 Nm ³ /h, the reaction temperature was 430°C, the reaction pressure was 0.04 MPa, and the propylene-ammonia-air ratio was 1:1.2:9.6.

As a result of operating the device, the following data were obtained: the yield of acrylonitrile was 80.5%, and the degree of propylene conversion was 98.5%.

Example 5

As illustrated in FIG. 4, in the fluidized bed reactor, the diameter was 8 m, the tangential height was 18 m (i.e., the total height of the dense phase zone and the dilute phase zone, which are illustrated in Fig. 1), the filling was 160 tons of SANC series acrylonitrile synthesis catalyst , which is supplied by Shanghai Petrochemical Technology Research Institute SINOPEC, and inside there were 110 U-shaped heat sink water pipes, which were divided into 20 groups, and each group was formed by connecting two U-shaped, five U-shaped and six U-shaped heat-removing water pipes arranged in series, with the outer diameter of the straight pipeline section of each heat-removing water pipe being 114 mm, the length of the straight pipeline section being 10 m, and the gap between the pipes being 220 mm; and inside there were 28 cyclone separators, which were divided into 14 sets, each of which contained two stages of cyclone separators connected in series, and the outer diameters of the first stage and second stage risers were 326 mm and 219 mm, respectively, the length of the first riser the stage was 12.0 m, and the length of the second stage riser was 10.1 m.

The ratio of the number of cooling water lines to the number of cyclone separator drain risers in the fluidized bed reactor was 7.85.

In the reaction cooling section of the fluidized bed reactor, the diameter was 8 m and the length L was 7.4 m. At the center point of the reaction cooling section, L1/S1 = 2.04 m ^-1 , L2/S1 = 1.57 m ^-1 and L3/S1 = 0.48 m ^-1 .

The pressure pulsation intensity data was measured at _H0 = 2 m, and the graph of the pressure pulsation intensity data was similar to the graph in Example 2.

The device was operated under the following conditions: the propylene injection rate was 5900 Nm ³ /h, the reaction temperature was 430°C, the reaction pressure was 0.04 MPa, and the propylene-ammonia-air ratio was 1:1.2:9.6.

As a result of operating the device, the following data were obtained: the yield of acrylonitrile was 79.3%, and the degree of propylene conversion was 96.8%.

Example 6

As illustrated in FIG. 4, in the fluidized bed reactor, the diameter was 8 m, the tangential height was 18 m (i.e., the total height of the dense phase zone and the dilute phase zone, which are illustrated in Fig. 1), the filling was 160 tons of SANC series acrylonitrile synthesis catalyst , which is supplied by Shanghai Petrochemical Technology Research Institute SINOPEC, and inside there were 266 U-shaped heat sink water pipes, which were divided into 48 groups, and each group was formed by connecting two U-shaped, five U-shaped and six U-shaped heat-removing water pipes arranged in series, with the outer diameter of the straight pipeline section of each heat-removing water pipe being 114 mm, the length of the straight pipeline section being 10 m, and the gap between the pipes being 215 mm; and inside there were 18 cyclone separators, which were divided into 9 sets, each of which contained two stages of cyclone separators connected in series, and the outer diameters of the first stage and second stage risers were 326 mm and 219 mm, respectively, the length of the first stage riser the stage was 12.0 m, and the length of the second stage riser was 10.1 m.

The ratio of the number of cooling water lines to the number of cyclone separator drain risers in the fluidized bed reactor was 29.55.

In the reaction cooling section of the fluidized bed reactor, the diameter was 8 m and the length L was 7.4 m. At the center point of the reaction cooling section, L1/S1 = 4.10 m ^-1 , L2/S1 = 3.79 m ^-1 and L3/S1 = 0.31 m ^-1 .

- 13 046737

The pressure pulsation intensity data was measured at H0 = 2 m, and the graph of the pressure pulsation intensity data was similar to that of Example 3.

The device was operated under the following conditions: the propylene injection rate was 5900 Nm ³ /h, the reaction temperature was 430°C, the reaction pressure was 0.04 MPa, and the propylene-ammonia-air ratio was 1:1.2:9.6.

As a result of operating the device, the following data were obtained: the yield of acrylonitrile was 80.5%, and the degree of propylene conversion was 98.6%.

Example 7

As illustrated in FIG. 4, in the fluidized bed reactor, the diameter was 8 m, the tangential height was 18 m (i.e., the total height of the dense phase zone and the dilute phase zone, which are illustrated in Fig. 1), the filling was 160 tons of SANC series acrylonitrile synthesis catalyst , which is supplied by Shanghai Petrochemical Technology Research Institute SINOPEC, and inside there were 225 U-shaped heat sink water pipes, which were divided into 40 groups, and each group was formed by connecting two U-shaped, five U-shaped and six U-shaped heat-removing water pipes arranged in series, with the outer diameter of the straight pipeline section of each heat-removing water pipe being 114 mm, the length of the straight pipeline section being 10 m, and the gap between the pipes being 220 mm; and internally there were 12 cyclone separators, which were divided into 4 sets, each containing three stages of cyclone separators connected in series, the outer diameters of the first stage, second stage and third stage risers being 326 mm, 219 mm and 219 mm, Accordingly, the length of the first stage riser was 12.0 m, and the length of the second stage and third stage risers was 10.1 m.

In the reaction cooling section of the fluidized bed reactor, the diameter was 8 m and the length L was 7.4 m. At the center point of the reaction cooling section, L1/S1 = 3.40 m ^-1 , L2/S1 = 3.21 m ^-1 and L3/S1 = 0.19 m ^-1 .

The pressure pulsation intensity data was measured at _H0 = 2 m, and the graph of the pressure pulsation intensity data was similar to the graph in Example 1.

The device was operated under the following conditions: the propylene injection rate was 5900 Nm ³ /h, the reaction temperature was 430°C, the reaction pressure was 0.04 MPa, and the propylene-ammonia-air ratio was 1:1.2:9.6.

As a result of operating the device, the following data were obtained: the yield of acrylonitrile was 79.5%, and the degree of propylene conversion was 97.6%.

Example 8

As illustrated in FIG. 4, in the fluidized bed reactor, the diameter was 8 m, the tangential height was 18 m (i.e., the total height of the dense phase zone and the dilute phase zone, which are illustrated in Fig. 1), the filling was 160 tons of SANC series acrylonitrile synthesis catalyst , which is supplied by Shanghai Petrochemical Technology Research Institute SINOPEC, and inside there were 225 U-shaped heat sink water pipes, which were divided into 40 groups, and each group was formed by connecting two U-shaped, five U-shaped and six U-shaped heat-removing water pipes arranged in series, with the outer diameter of the straight pipeline section of each heat-removing water pipe being 114 mm, the length of the straight pipeline section being 10 m, and the gap between the pipes being 220 mm; and inside there were 24 cyclone separators, which were divided into 8 sets, each of which contained three stages of cyclone separators connected in series, and the outer diameters of the first stage, second stage and third stage risers were 326 mm, 219 mm and 219 mm, Accordingly, the length of the first stage riser was 12.0 m, and the length of the second stage and third stage risers was 10.1 m.

In the reaction cooling section of the fluidized bed reactor, the diameter was 8 m and the length L was 7.4 m. At the center point of the reaction cooling section, L1/S1 = 3.23 m ^-1 , L2/S1 = 2.85 m ^-1 and L3/S1 = 0.38 m ^-1 .

The pressure pulsation intensity data was measured at _H0 = 2 m, and the graph of the pressure pulsation intensity data was similar to the graph in Example 1.

The device was operated under the following conditions: the propylene injection rate was 5900 Nm ³ /h, the reaction temperature was 430°C, the reaction pressure was 0.04 MPa, and the propylene-ammonia-air ratio was 1:1.2:9.6.

As a result of operating the device, the following data were obtained: the yield of acrylonitrile was 80.2%, and the degree of propylene conversion was 98.1%.

Example 9

As illustrated in FIG. 4, in the fluidized bed reactor, the diameter was 8 m, the tangential height was 18 m (i.e., the total height of the dense phase zone and the dilute phase zone

- 14 046737 phases, which are illustrated in Fig. 1), the filling was 160 tons of SANC series acrylonitrile synthesis catalyst supplied by Shanghai Petrochemical Technology Research Institute SINOPEC, and there were 140 U-shaped heat sink water pipes, which were divided into 26 groups, and each group was formed by connecting two U --shaped, five U-shaped and six U-shaped heat-removing water pipes arranged in series, and the outer diameter of the straight pipeline section of each heat-removing water pipe was 114 mm, and the length of the straight pipeline section was 8 m; and inside there were 18 cyclone separators, which were divided into 9 sets, each of which contained two stages of cyclone separators connected in series, and the outer diameters of the first stage and second stage risers were 326 mm and 219 mm, respectively, the length of the first riser the stage was 12.0 m, and the length of the second stage riser was 10.1 m.

In the reaction cooling section of the fluidized bed reactor, the diameter was 8 m and the length L was 7.2 m. At the center point of the reaction cooling section, L1/S1 = 2.28 m ^-1 , L2/S1 = 2.00 m ^-1 and L3/S1 = 0.29 m ^-1 .

The pressure pulsation intensity data was measured at H0 = 2 m, and the graph of the pressure pulsation intensity data was similar to the graph in Example 2.

The device was operated under the following conditions: the propylene injection rate was 5900 Nm ³ /h, the reaction temperature was 430°C, the reaction pressure was 0.04 MPa, and the propylene-ammonia-air ratio was 1:1.2:9.6.

As a result of operating the device, the following data were obtained: the yield of acrylonitrile was 79.6%, and the degree of propylene conversion was 97.3%.

Example 10

As illustrated in FIG. 4, in the fluidized bed reactor, the diameter was 8 m, and the tangential height was 18 m (i.e., the total height of the dense phase zone and the dilute phase zone, which are illustrated in Fig. 1), the filling was 160 tons of acrylonitrile synthesis catalyst series SANC, which is supplied by Shanghai Petrochemical Technology Research Institute SINOPEC, and inside there were 190 U-shaped heat sink water pipes, which were divided into 34 groups, with each group formed by connecting two U-shaped, five U-shaped and six U-shaped shaped heat sink pipes arranged in series, wherein the outer diameter of the straight pipe section of each heat sink pipe was 114 mm, the length (Lz) of the straight pipe section was 8 m, and fins were present on the outside of the pipe walls of the 95 straight pipe sections, as illustrated in FIG. 5f, wherein 4 fins were evenly distributed on the outer pipe wall, and the fins had a length (Lt) of 3000 mm, a height of 10 mm, and a width of 20 mm. In addition, 22 cyclone separators were present inside the fluidized bed reactor, which were divided into 11 sets, each containing two stages of cyclone separators connected in series, with the outer diameters of the first stage and second stage risers being 326 mm and 219 mm. Accordingly, the length of the first stage riser was 12.0 m, and the length of the second stage riser was 10.1 m.

In the reaction cooling section of the fluidized bed reactor, the diameter was 8 m and the length L was 7.4 m. At the center point of the reaction cooling section, L1/S1 = 3.12 m ^-1 , L2/S1 = 2.75 m ^-1 and L3/S1 = 0.37 m ^-1 .

The pressure pulsation intensity data was measured at _H0 = 2 m, and the graph of the pressure pulsation intensity data was similar to the graph in Example 1.

The device was operated under the following conditions: the propylene injection rate was 5900 Nm ³ /h, the reaction temperature was 430°C, the reaction pressure was 0.04 MPa, and the propylene-ammonia-air ratio was 1:1.2:9.6.

As a result of operating the device, the following data were obtained: the yield of acrylonitrile was 80.7%, and the degree of propylene conversion was 98.8%.

Example 11

As illustrated in FIG. 4, in the fluidized bed reactor, the diameter was 8 m, and the tangential height was 18 m (i.e., the total height of the dense phase zone and the dilute phase zone, which are illustrated in Fig. 1), the filling was 160 tons of acrylonitrile synthesis catalyst series SANC, which is supplied by Shanghai Petrochemical Technology Research Institute SINOPEC, and inside there were 190 U-shaped heat sink water pipes, which were divided into 34 groups, with each group formed by connecting two U-shaped, five U-shaped and six U-shaped shaped heat sink pipes arranged in series, wherein the outer diameter of the straight pipe section of each heat sink pipe was 114 mm, the length (Lz) of the straight pipe section was 8 m, and fins were present on the outside of the pipe walls of the 95 straight pipe sections, as illustrated in FIG. 5a, with 8 fins distributed along the outer pipe wall, and the vertical

- 15 046737 the gap between the ribs was 500 mm, and the angle α1 was 50°. The ribs had a length (Lt) of 3500 mm, a height of 10 mm, and a width of 20 mm. In addition, 20 cyclone separators were present inside the fluidized bed reactor, which were divided into 10 sets, each containing two stages of cyclone separators connected in series, with the outer diameters of the first stage and second stage risers being 326 mm and 219 mm. Accordingly, the length of the first stage riser was 12.0 m, and the length of the second stage riser was 10.1 m.

In the reaction cooling section of the fluidized bed reactor, the diameter was 8 m and the length L was 7.4 m. At the center point of the reaction cooling section, L1/S1 = 3.15 m ^-1 , L2/S1 = 2.78 m ^-1 and L3/S1 = 0.37 m ^-1 .

The pressure pulsation intensity data was measured at H0 = 2 m, and the graph of the pressure pulsation intensity data was similar to that of Example 1.

The device was operated under the following conditions: the propylene injection rate was 5900 Nm ³ /h, the reaction temperature was 430°C, the reaction pressure was 0.04 MPa, and the propylene-ammonia-air ratio was 1:1.2:9.6.

As a result of operating the device, the following data were obtained: the yield of acrylonitrile was 80.6%, and the degree of propylene conversion was 98.7%.

Example 12

As illustrated in FIG. 4, in the fluidized bed reactor, the diameter was 8 m, the tangential height was 18 m (i.e., the total height of the dense phase zone and the dilute phase zone, which are illustrated in Fig. 1), the filling was 160 tons of SANC series acrylonitrile synthesis catalyst , which is supplied by Shanghai Petrochemical Technology Research Institute SINOPEC, and inside there were 225 U-shaped heat sink water pipes, which were divided into 40 groups, and each group was formed by connecting two U-shaped, five U-shaped and six U-shaped heat-removing water pipes arranged in series, with the outer diameter of the straight pipeline section of each heat-removing water pipe being 114 mm, and the length of the straight pipeline section being 8 m; and inside there were 42 cyclone separators, which were divided into 21 sets, each of which contained two stages of cyclone separators, connected, arranged in series, and the outer diameters of the first stage and second stage drain risers were, respectively, 400 mm and 325 mm, length The length of the first stage riser was 12.0 m, and the length of the second stage riser was 10.1 m.

In the reaction cooling section of the fluidized bed reactor, the diameter was 8 m and the length L was 7.2 m. At the center point of the reaction cooling section, L1/S1 = 4.16 m ^-1 , L2/S1 = 3.21 m ^-1 and L3/S1 = 0.95 m ^-1 .

The pressure pulsation intensity data was measured at _H0 = 2 m, and the graph of the pressure pulsation intensity data was similar to the graph in Example 1.

The device was operated under the following conditions: the propylene injection rate was 5900 Nm ³ /h, the reaction temperature was 430°C, the reaction pressure was 0.04 MPa, and the propylene-ammonia-air ratio was 1:1.2:9.6.

As a result of operating the device, the following data were obtained: the yield of acrylonitrile was 80.1%, and the degree of propylene conversion was 98.7%.

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Claims (16)

CLAIM 1. A fluidized bed reactor comprising at least a reaction cooling section and a vertical internal component present in the reaction cooling section, wherein the length of the reaction cooling section in a direction along the central axis of the fluidized bed reactor is designated as L, expressed in units of m , then at an arbitrary position within the region from 49% L above the center point of the reaction cooling section to 49% L below the center point of the reaction cooling section, the cross-sectional area running perpendicular to the central axis of the fluidized bed reactor of the reaction cooling section is designated as S1, expressed in units of m ² , and the circumference of the outer contour of the cross section running perpendicular to the central axis of the fluidized bed reactor of the vertical internal component is designated as L1, expressed in units of m, and when multiple cross sections are present, this means the sum of the circumferences of the outer contour of all cross sections sections, then L1/S1 = 2.0-4.3 m ^-1 , and the vertical internal component is a heat removal pipeline or a combination of a heat removal pipeline and a gas-solid phase separator. 2. The fluidized bed reactor according to claim 1, wherein the vertical internal component is a heat removal conduit, wherein the cross-sectional area of the reaction cooling section is designated S1, expressed in units of m ² , and the circumference of the outer contour of the cross-section extending perpendicular to the central The axis of the fluidized bed reactor, the heat removal pipeline in terms of a straight pipeline section is designated as L2, expressed in units of m, and when there are many cross sections, this means the sum of the circumferences of the outer contour of all cross sections, then L2/S1 = 1.7- 3.6 m ^-1 , and the vertical internal component optionally further comprises a gas-solid separator, wherein the cross-sectional area of the reaction cooling section is designated as S1, expressed in units of m ² , and the circumference of the outer contour of the cross-section extending perpendicular to the central axis fluidized bed reactor, gas-solid separator in terms of the riser is designated as L3, expressed in units of m, and when there are many cross sections, this means the sum of the circumferences of the outer contour of all cross sections, then L3/S1 = 0.25 -0.85 m ^-1 . 3. The fluidized bed reactor according to claim 2, wherein the cross sections are obtained at an arbitrary position within the region from 45% L above the center point of the reaction cooling section to 38% L below the center point of the reaction cooling section, and/or L1/S1 = 2.2-4.1 m ^-1 , and/or L2/S1 = 1.9-3.5 m ^-1 , and/or the gas-solid separator is a cyclone separator, and/or L3/S1 = 0 .30-0.75 m ^-1 . 4. The fluidized bed reactor according to claim 1, in which the number of heat removal pipelines in terms of a straight pipeline section is 220-5000, and/or the number of gas and solid separators in terms of a riser is 16-516, and/or the ratio the number of straight pipeline sections to the number of drain risers is 8.5-24.0. 5. The fluidized bed reactor according to claim 4, in which the number of heat removal pipelines in terms of a straight pipeline section is 300-2400, and/or the number of gas and solid separators in terms of a riser is 16-210, and/or the ratio the number of straight pipeline sections to the number of drain risers is 11.5-21.0. 6. The fluidized bed reactor according to claim 4, wherein the outer diameters of the straight pipe sections, which are the same or different from each other, are in each case independently from 80 to 180 mm, and/or the inner diameters of the straight pipe sections, which are the same or different from each other, in each case independently ranging from 60 to 150 mm, and/or the lengths of straight pipeline sections that are the same or different from each other, in each case independently ranging from 4.0 to 13 m, and/ or the outer diameters of the risers, which are the same or different from each other, in each case independently from 150 to 410 mm, and/or the inner diameters of the risers, which are the same or different from each other, in each case independently from 130 up to 400 mm, and/or the lengths of the risers, which are the same or different from each other, in each case independently range from 6 to 14 m, and/or the reaction cooling section has a diameter from 5 to 29 m, area S1 is from 19 .6 to 660 ^m2 , and/or length L is from 4 to 12.5 m. 7. The fluidized bed reactor according to claim 6, wherein the outer diameters of the straight pipe sections are in each case independently from 90 to 170 mm, and/or the inner diameters of the straight pipe sections are in each case independently from 70 to 140 mm, and/ or the lengths of straight pipeline sections in each case independently range from 5.5 to 12.0 m, and/or the outer diameters of the risers in each case independently range from 200 to 360 mm, and/or the internal diameters of the risers in each case independently amount to from 180 to 350 mm, and/or the lengths of the risers in each case independently range from 10 to 13 m, and/or the reaction cooling section - 17 046737 has a diameter of 7 to 20 m and/or an area S1 of 38.5 to 314 m ² and/or a length L of 5.5 to 11.5 m. 8. The fluidized bed reactor according to claim 1, which comprises a head section, a dilute phase zone, a reaction cooling section, a pre-reaction section and a cone in order from top to bottom, and further comprises a gas distribution plate and optionally a fluid distributor present in the pre-reaction section sections. 9. The fluidized bed reactor according to claim 1, wherein the reaction cooling section has a substantially circular cross-section, and/or the cross-section of the vertical inner component has a substantially circular inner contour and a substantially circular outer contour, and/or the cross-section of the vertical inner component has a substantially circular inner loop and a substantially circular outer loop comprising one or more projections, and/or the vertical inner component comprises a heat sink conduit, the heat sink conduit having a heat sink medium inlet, n straight conduit sections, and a heat sink medium outlet, wherein the head end of the first straight conduit section is in communication with the inlet of the heat-removing medium, the tail end of the n-th straight pipeline section is in communication with the outlet of the heat-removing medium, the tail end of the i-th straight pipeline section is in communication with the head end of the (|+1)-th straight pipeline section through U- a shaped pipe, wherein n is an integer from 2 to 100, i is an arbitrary integer between 1 and n-1, and there are one or more projections on the outer wall of some or all of the straight pipe sections. 10. The fluidized bed reactor according to claim 9, wherein said straight pipe section is a straight circular pipe section, and/or n is an integer from 2 to 20, and/or one or more projections are present on the outer wall 10- 40% straight pipe sections. 11. The fluidized bed reactor according to claim 9, wherein the outer diameters of the straight pipe sections, which are the same or different from each other, are in each case independently 80-180 mm, and/or the inner diameters of the straight pipe sections, which are the same or differ from each other, in each case independently amount to 60-150 mm, and/or the lengths of straight pipeline sections that are the same or different from each other, in each case independently amount to 4.0-13.0 m, and/or the center lines of any two adjacent straight pipe sections are parallel to each other, and the distances between the center lines of any two adjacent straight pipe sections are the same or different from each other, and in each case are independently 160-540 mm. 12. The fluidized bed reactor according to claim 11, in which the outer diameters of the straight pipe sections in each case are independently 90-170 mm, and/or the inner diameters of the straight pipe sections in each case are independently 70-140 mm, and/or the lengths straight pipeline sections in each case are independently 5.5-12.0 m, and/or the distances between the center lines of any two adjacent straight pipeline sections are the same, and/or in each case are independently 180-430 mm. 13. The fluidized bed reactor of claim 9, wherein the one or more projections extend in a continuous or intermittent manner in a direction along the center line of the straight pipe section, and/or the one or more projections extend in a continuous or discontinuous manner around the center line of the straight pipe section. 14. The fluidized bed reactor according to claim 13, wherein the one or more projections extend in a continuous or discontinuous manner around the center line of the straight pipe section in the form of a ring or helix. 15. The fluidized bed reactor according to claim 9, wherein in the case where one or more protrusions extend in a continuous or discontinuous manner in a direction along the center line of the straight pipe section, the travel length Lt of the one or more protrusions is not more than the length Lz of the straight pipe section sections, and/or when one or more projections extend in a continuous or intermittent manner around the center line of a straight pipe section in the form of a ring, the height Hh of the ring is not more than the length Lz of the straight pipeline section, or when one or more projections extend in a continuous or discontinuous manner around the center line of the straight pipe section in the form of a spiral, the height Ht of the spiral is not more than the length Lz of the straight pipe section, and/or the height of one or more projections is from 0.005 times to 0.3 times the outer diameter of the straight pipe section, and/or the width of one or more projections is from 0.005 times to 0.3 times the outer diameter of the straight pipe section. 16. The fluidized bed reactor according to claim 15, wherein Lt/Lz is from 0.1 to 0.6, and/or Hh/Lz is from 0.01 to 0.3, and/or Ht/Lz is from 0.2 to 0.6, and/or the height of one or more projections is from 0.008 times to 0.1 times the outer diameter of the straight pipeline section, and/or the width of one or more projections is from 0.008 times to 0.2 -multiple -