Internal components for a dense phase gas-solids fluidized bed and a dense phase gas-solids fluidized bed and fluidization method

Abstract

The application provides an inner component for a gas-solid dense phase fluidized bed, which comprises a bed body, a gas inlet, a gas distributor, a gas outlet and a gas-solid separation device; the bed body comprises a dense phase section bed body and a diameter expansion section bed body from bottom to top, and the inner diameter of the diameter expansion section bed body is larger than that of the dense phase section bed body; the inner component is coaxially arranged in the bed body; the inner component comprises a bubble breaking structure which is a continuous structure or an intermittent structure and is coaxially arranged with the bed body. The inner component can be applied to a gas-solid dense phase fluidized bed with a small inner diameter dense phase section bed body and a large height-diameter ratio catalyst bed layer, effectively solves the problem of gas surge, and improves the fluidization quality of solid particles. The application also provides a gas-solid dense phase fluidized bed with the aforementioned inner component and a fluidization method thereof, and the problem of gas surge can be effectively solved by using the aforementioned inner component.

Description

Technical Field

[0001] This invention belongs to the field of fluidized beds, specifically relating to internal components for gas-solid dense phase fluidized beds, gas-solid dense phase fluidized beds, and fluidization methods. Background Technology

[0002] Fluidization refers to the process of dispersing and suspending solid particles using gas and / or liquid, thereby transforming them into fluid-like properties. Currently, fluidization technology is widely used as a fundamental technology in various physical and chemical processes. Depending on the fluidizing medium and fluidization velocity, various fluidization states can be observed. Among them, gas-solid dense-phase fluidized beds have advantages such as high particle mixing, uniform bed temperature and concentration, and high mass and heat transfer efficiency, and are widely used in industries such as coal processing and utilization, petrochemicals, fine chemicals, metallurgy, and mineral processing.

[0003] In fluidization processes with low gas velocities, bubble coalescence and breakup are constant occurrences. When the bubble size grows large enough compared to the bed diameter, gas plugs form, resulting in an alternating state of gas plugs and particle plugs in the entire bed—this is known as throttling. Throttling typically occurs in beds with small diameters (here, diameter refers to the inner diameter of the dense phase bed) and large aspect ratios (here, aspect ratio refers to the aspect ratio of the catalyst bed). Throttling leads to a significant decrease in heat and mass transfer efficiency, increased particle-wall friction, increased momentum loss, increased bed pressure drop fluctuations, and increased bed vibration amplitude, severely impacting fluidization performance and operational stability.

[0004] With the advancement of reaction and process control technologies towards refinement, small-diameter fluidized beds are finding increasingly widespread applications. However, the degree of slugging in small-diameter fluidized beds is significantly higher than that in large-diameter fluidized beds. Currently, adding internal components is commonly used to suppress slugging, but the effectiveness of suppressing slugging varies depending on the size of the fluidized bed and the type of internal component used. CN201911095519.1 discloses an internal component and a multi-stage fluidized bed reactor. This internal component is applied within the chamber of the fluidized bed reactor and includes: a shell with an outer wall of a first conical structure and a fixed connection structure, wherein the conical end of the shell is closed; an opening is provided at the bottom end of the first conical structure corresponding to the conical end, and the opening faces downward within the chamber; the fixed connection structure is disposed on the outer wall of the shell and fixedly connected to the fluidized bed reactor, so that the shell of the first conical structure divides the chamber into at least two reaction zones with upper and lower structures. While the internal component provided by this invention can disrupt large bubbles and suppress the formation of nodding in a high aspect ratio fluidized bed to some extent, it also causes particles to form a partially high-concentration zone at the bottom and a low-concentration zone at the top, resulting in uneven particle dispersion and affecting heat and mass transfer. Furthermore, the obstruction caused by the internal component increases particle collision wear and backmixing. CN202110381412.4 discloses a device that divides a single-chamber nodding fluidized bed into several independent seepage fluidized beds along the height direction. During fluidization, nodding occurs in the lower chamber, pushing the particle layer through the intermediate partition and air distribution plate into the upper chamber, forming a special flow pattern of first seeping and then permeating. This fluidized bed structure decomposes the large and intense nodding in a single bed into small and regular seepage, prolonging the residence time of solid particles, reconstructing the fluidization state of the upper chamber, reducing backmixing, and improving the gas-solid mixing characteristics within the reactor. However, there is still a bottleneck area between the two baffles, and the fluidization state is only improved in the upper part of the baffle. In addition, due to the presence of the baffle, particles must pass through the pores on the baffle to rise, which increases the friction with the baffle, making solid particles easier to break and increasing the pressure drop of the bed. Although the existing technology can suppress bottlenecks to some extent, the suppression effect is weak and cannot effectively solve the bottleneck problem. Moreover, due to the effect of the internal structure, new problems may arise. Furthermore, the internal components provided by the existing technology are generally suitable for large-diameter fluidized beds, but not for fluidized beds with small diameters (here, diameter refers to the inner diameter of the dense phase bed) and large aspect ratio catalyst beds. Summary of the Invention

[0005] The first objective of this invention is to provide an internal component for a gas-solid dense phase fluidized bed, which is suitable for use in gas-solid dense phase fluidized beds with small inner diameter dense phase section beds and large height-to-diameter ratio catalyst beds, and is used to effectively solve the problem of throttling.

[0006] A second objective of the present invention is to provide a gas-solid dense-phase fluidized bed having the aforementioned internal components.

[0007] The third objective of this invention is to provide a fluidization method for dense-phase fluidization of solid particles using the aforementioned gas-solid dense-phase fluidized bed.

[0008] To achieve the first objective of this invention, the following technical solution is adopted:

[0009] An internal component for a gas-solid dense phase fluidized bed, the gas-solid dense phase fluidized bed comprising a bed body, a gas inlet, a gas distributor, a gas outlet, and a gas-solid separation device; the bed body comprises a dense phase section bed body from bottom to top and an expanding diameter section bed body, the inner diameter of the expanding diameter section bed body being larger than the inner diameter of the dense phase section bed body;

[0010] The internal components are coaxially disposed within the bed body;

[0011] The internal components include a bubble-breaking structure, which can be a continuous or discontinuous structure and is coaxially arranged with the bed body.

[0012] Preferably, the bubble-breaking structure is a spiral structure.

[0013] Preferably, the helical structure is a continuous structure, including a threaded structure, a linear helical structure, or a sheet-like helical structure; or

[0014] The spiral structure is an intermittent structure, including multiple legs, which are arranged in a spiral pattern at intervals within the bed body. The angle between the central axis of the legs and the plane perpendicular to the central axis of the dense phase section of the bed body is less than 30°.

[0015] Preferably, the outer diameter D of the spiral structure 螺外 The inner diameter D of the dense phase section bed body 密内 The ratio D 螺外 / D 密内 =0.5-0.95; and / or

[0016] The pitch L1 of the spiral structure is related to the inner diameter D of the dense phase section bed. 密内 The ratio L1 / D 密内 =0.5-2.

[0017] Preferably, the distance L2 between the internal component and the gas distributor is equal to the inner diameter D of the dense phase section bed. 密内 The ratio L2 / D 密内 ≤3; and / or

[0018] The ratio of the height H1 of the internal component to the height H2 of the dense phase section bed body is H1 / H2 ≥ 80%.

[0019] In one embodiment, the internal component further includes an internal component body, which is coaxially disposed with the bed body;

[0020] The bubble-breaking structure is disposed along the outer surface of the main body of the internal component.

[0021] Preferably, the ratio of the cross-sectional area S1 of the main body of the internal component to the cross-sectional area S2 of the dense phase section bed body is S1 / S2 = 1-50%.

[0022] In one embodiment, the defoaming structure is disposed along the inner wall of the dense phase section bed.

[0023] To achieve the second objective of the present invention, a gas-solid dense-phase fluidized bed having the aforementioned internal components is also provided.

[0024] Preferably, in the gas-solid dense-phase fluidized bed, the height H2 of the dense-phase section of the bed and its inner diameter D are... 密内 The ratio H2 / D 密内 ≥3;

[0025] Preferably, in the gas-solid dense-phase fluidized bed, the inner diameter D of the dense-phase section of the bed is... 密内 ≤150mm, catalyst bed height-to-diameter ratio >10.

[0026] To achieve the second objective of this invention, a method for dense-phase fluidization of solid particles using the aforementioned gas-solid dense-phase fluidized bed is also provided.

[0027] The beneficial effects of this invention are as follows:

[0028] The internal component for a gas-solid dense phase fluidized bed of the present invention can be used in a gas-solid dense phase fluidized bed, and can be applied to a gas-solid dense phase fluidized bed with a small inner diameter (e.g., ≤150mm) dense phase section and a large height-to-diameter ratio (e.g., >10) catalyst bed. When solid particles are densely fluidized using a gas-solid dense phase fluidized bed with this internal component, bubbles can be effectively broken, slugging can be suppressed, pressure fluctuations can be reduced, and fluidization quality can be improved. Stable fluidization of particles in a gas-solid dense phase fluidized bed with a small inner diameter (e.g., ≤150mm) dense phase section and a large height-to-diameter ratio (e.g., >10) catalyst bed can be achieved. Attached Figure Description

[0029] Figure 1 This is a schematic diagram of the internal components of the present invention used in a gas-solid dense phase fluidized bed in one embodiment;

[0030] Figure 2 This is a schematic diagram of the internal components of the present invention used in a gas-solid dense phase fluidized bed in another embodiment;

[0031] Figure 3This is a schematic diagram of the structure of the gas-solid dense phase fluidized bed in one embodiment of the present invention;

[0032] Figure 4 This is a schematic diagram of the gas-solid dense-phase fluidized bed in another embodiment of the present invention;

[0033] Figure 5 This is a graph showing the variation of bed pressure drop in the gas-solid dense phase fluidized bed with sampling time in Embodiment 1 of the present invention;

[0034] Figure 6 This is a graph showing the variation of bed pressure drop in the gas-solid dense phase fluidized bed with sampling time in Embodiment 2 of the present invention;

[0035] Figure 7 This is a graph showing the variation of bed pressure drop of the gas-solid dense phase fluidized bed in Comparative Example 1 of this invention with sampling time;

[0036] Figure 8 This is a graph showing the variation of bed pressure drop of the gas-solid dense phase fluidized bed in Comparative Example 2 of this invention with sampling time. Detailed Implementation

[0037] The technical solution and its effects of the present invention will be further described below with reference to specific embodiments / examples. The following embodiments / examples are only for illustrating the content of the present invention, and the invention is not limited to the following embodiments or examples. Simple modifications made to the present invention based on the concept of the present invention are all within the scope of protection claimed by the present invention.

[0038] An internal component for a gas-solid dense-phase fluidized bed, such as Figure 1-4 As shown, the gas-solid dense phase fluidized bed includes a bed body, a gas inlet 1, a gas distributor 2, a gas outlet 6, and a gas-solid separation device 7; the bed body includes a dense phase section bed body 3 from bottom to top and an expansion section bed body 4, wherein the inner diameter of the expansion section bed body 4 is larger than the inner diameter of the dense phase section bed body 3;

[0039] The internal component 5 is coaxially disposed within the bed body;

[0040] The internal component 5 includes a bubble-breaking structure 51, which is a continuous or discontinuous structure and is coaxially arranged with the bed body.

[0041] The internal components of this invention, through the bubble-breaking structure 51 coaxially arranged with the bed body, can block large bubbles generated during fluidization, thereby breaking them into smaller bubbles, effectively suppressing the occurrence of slugging and forming a stable particulate dense phase bed within the dense phase section. The coaxial arrangement of the internal components with the bed body facilitates efficient bubble breaking.

[0042] Those skilled in the art will understand that in the gas-solid dense phase fluidized bed, the gas inlet 1 is located at the bottom of the dense phase section bed 3, and the gas distributor 2 is located between the gas inlet 1 and the dense phase section bed 3; the gas-solid separation device 7 is located at the upper part of the expansion section bed 4. In one embodiment, the gas-solid separation device 7 has an outlet pipe at its top; the outlet pipe extends from the top of the expansion section bed 4 to form the gas outlet 6.

[0043] Those skilled in the art will understand that the gas distributor is a commonly used gas distributor in the field. In one embodiment, the gas distributor is a perforated plate gas distributor, a tubular gas distributor, or a packed gas distributor, used to uniformly distribute the gas entering the fluidized bed.

[0044] Those skilled in the art will understand that the gas-solid separation device is used to separate solid particles entrained in a gas from the gas.

[0045] Those skilled in the art will understand that the dense phase section bed 3 can be any structure suitable for the art, such as a conical bed, a cylindrical bed, or a bed with a conical lower section and a cylindrical upper section. Of course, a cylindrical bed is the most common.

[0046] The internal components of this invention can be applied to gas-solid dense phase fluidized beds, and are applicable to gas-solid dense phase fluidized beds with small inner diameter (e.g., ≤150mm) dense phase section beds and large height-to-diameter ratio (e.g., >10) catalyst beds, to solve their surge problems.

[0047] In this invention, the height-to-diameter ratio of the catalyst bed is equal to the height-to-diameter ratio of the catalyst bed in the dense phase section of the bed, which is equal to the height of the catalyst bed in the dense phase section of the bed and the equivalent diameter of the catalyst bed cross section.

[0048] In this invention, "the height of the catalyst bed" refers to the "height of the dense phase catalyst bed" after the catalyst is fluidized.

[0049] In this invention, the bubble-breaking structure 51 can be a spiral structure, a multi-layered arrangement structure, a bent structure, a multi-shape combination structure, or any other structure that can achieve bubble breaking.

[0050] In one embodiment, the bubble-breaking structure 51 is a spiral structure.

[0051] In one embodiment, the helical structure is a continuous structure, including a threaded structure, a linear helical structure, or a sheet-like helical structure. Alternatively...

[0052] In one embodiment, the spiral structure is an intermittent structure, including multiple legs, which are arranged in a spiral interval within the bed body. The angle between the central axis of the legs and the plane perpendicular to the central axis of the dense phase section bed body 3 is <30°, such as 29°, 25°, 20°, 15°, 10°, and 5°.

[0053] Those skilled in the art will understand that the outrigger can be any shape suitable for use in the art. In one embodiment, the cross-section of the outrigger is circular, triangular, quadrilateral, or polygonal.

[0054] In one embodiment, the support leg is a cylindrical support leg or an n-prism support leg, where n≥3, such as 3, 4, 5, 6, 7, etc. Correspondingly, the support leg is a triangular prism support leg, a quadrangular prism support leg, a pentagonal prism support leg, a hexagonal prism support leg, a heptagonal prism support leg, etc.

[0055] When n=4, the support leg is a quadrangular prism support leg, preferably a cuboid support leg.

[0056] In one embodiment, the outer diameter D of the helical structure 螺外 The inner diameter D of the dense phase section bed 3 密内 The ratio D 螺外 / D 密内 = 0.5-0.95, such as 0.55, 0.6, 0.65, 0.7, 0.75, 0.8, 0.85, and 0.9; and

[0057] The pitch L1 of the spiral structure is related to the inner diameter D of the dense phase bed 3. 密内 The ratio L1 / D 密内 =0.5-2, for example 0.6, 0.7, 0.8, 0.9, 1.0, 1.1, 1.3, 1.4, 1.5, 1.6, 1.7, 1.8 and 1.9.

[0058] Those skilled in the art will understand that pitch refers to the axial distance between two corresponding points on the pitch diameter of two adjacent threads. Therefore, in this invention, the pitch L1 of the helical structure refers to the axial distance between two corresponding points on the pitch diameter of two adjacent spiral coils.

[0059] In one embodiment, the distance L2 between the inner component 5 and the gas distributor 2 is equal to the inner diameter D of the dense phase bed 3. 密内 The ratio L2 / D 密内 ≤3, such as 0, 0.3, 0.6, 1, 1.5, 2, 2.5, and 3, etc.; and

[0060] The ratio H1 / H2 of the height H1 of the internal component 5 to the height H2 of the dense phase section bed body 3 is ≥80%, such as 85%, 90%, 95%, 100%, 105%, 110%, 115%, 120%, and 125%.

[0061] Those skilled in the art will understand that the distance L2 between the inner component 5 and the gas distributor 2 refers to the distance between the lower edge of the inner component 5 and the upper edge of the gas distributor 2.

[0062] In one embodiment, the internal component 5 further includes an internal component body 52, which is coaxially arranged with the bed body;

[0063] The bubble-breaking structure 51 is disposed along the outer surface of the inner component body 52.

[0064] Those skilled in the art will understand that when the bubble-breaking structure 51 is a spiral structure, it is spirally arranged along the outer surface of the inner component body 52.

[0065] For ease of fixation, in one embodiment, the inner component 5 (including the inner component body 52) extends beyond the gas-solid dense phase fluidized bed.

[0066] In one embodiment, the ratio of the cross-sectional area S1 of the inner component body 52 to the cross-sectional area S2 of the dense phase section bed body 3, S1 / S2, is 1-50%, such as 2%, 5%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, and 45%.

[0067] In another embodiment, the bubble-breaking structure 51 is disposed along the inner wall of the dense phase bed 3.

[0068] Those skilled in the art will understand that when the bubble-breaking structure 51 is a spiral structure, it is spirally arranged along the inner wall of the dense phase section bed 3.

[0069] The internal components of this invention can be used in gas-solid dense phase fluidized beds, and are applicable to gas-solid dense phase fluidized beds with small inner diameter dense phase sections and large aspect ratio catalyst beds, such as gas-solid dense phase fluidized beds with inner diameter ≤150mm and aspect ratio >10 catalyst beds. They can effectively break up bubbles generated due to throttling (the edges of the bubble-breaking structure can break up bubbles; the obstruction of the bubble-breaking structure can change the shape of bubbles during their ascent, such as increasing or decreasing size, thereby increasing disturbance and reducing the generation of large bubbles to a certain extent; it also changes the shape of the particle layer, increasing the breaking and collision of particle clusters), thereby suppressing throttling, reducing pressure fluctuations, and improving fluidization quality, enabling stable fluidization of solid particles in a gas-solid dense phase fluidized bed.

[0070] The present invention also provides a gas-solid dense-phase fluidized bed having the aforementioned internal components.

[0071] The gas-solid dense-phase fluidized bed of the present invention, having the aforementioned internal components, can effectively suppress slugging, thereby stabilizing the fluidization of solid particles entering it.

[0072] In one embodiment, in the gas-solid dense-phase fluidized bed, the height H2 of the dense-phase section bed 3 and its inner diameter D 密内 The ratio H2 / D 密内 ≥3, such as 3.1, 3.2, 3.3, 3.4, 3.5, 3.6, 3.7, 3.8, 3.9, 4, 4.5, 5, 5.5, 6, 10, 30, 60, 100 and 200, etc., and can also be larger.

[0073] In one embodiment, in the gas-solid dense-phase fluidized bed, the inner diameter D of the dense-phase section bed 3 is... 密内 ≤150mm, catalyst bed height-to-diameter ratio >10.

[0074] The present invention also provides a method for dense-phase fluidization of solid particles using the aforementioned gas-solid dense-phase fluidized bed.

[0075] In the method of this invention, the gaseous fluidizing medium is introduced into the gas-solid dense phase fluidized bed from the gas inlet 1 at the bottom. After passing through the gas distributor 2, it comes into contact with the solid particles in the gas-solid dense phase fluidized bed, causing the solid particles to fluidize. During the fluidization process, bubbles coalesce and break up. When large bubbles are generated, they are blocked by the internal component 5, and the large bubbles break into small bubbles, effectively suppressing the occurrence of slugging. A stable particle dense phase bed is formed in the dense phase section bed 3. The gas carries a small amount of fine particles into the expansion section bed 4, where the gas velocity decreases. Some of the fine particles settle back into the dense phase section bed 3, while some fine particles still enter the gas-solid separation device 7 with the gas for separation. The separated gas is led out through the gas outlet 6, and the separated particles are returned to the gas-solid dense phase fluidized bed.

[0076] The method of the present invention, by using a gas-solid dense phase fluidized bed with the internal component to perform dense phase fluidization of solid particles, can effectively break up bubbles, suppress slugging, reduce pressure fluctuations, and improve fluidization quality, and can achieve stable fluidization of particles in a gas-solid dense phase fluidized bed with a small inner diameter dense phase section and a large height-to-diameter ratio catalyst bed.

[0077] The present invention will be further illustrated below with specific embodiments and comparative examples.

[0078] Example 1 (S1)

[0079] use Figure 1 The internal components shown are Figure 3 The gas-solid dense-phase fluidized bed shown is used to fluidize solid particles; wherein...

[0080] The inner diameter D of the dense phase section bed 3 密内 =7mm, height H2 = 1m (H2 / D) 密内 ≥3); The inner component 5 includes a bubble-breaking structure 51 and an inner component body 52. ​​The inner component body 52 is cylindrical with an outer diameter of 3 mm. The bubble-breaking structure 51 is a spiral structure, including multiple legs, and the legs are cylindrical with a diameter of 1 mm and a length of 1.4 mm. The angle between the central axis of the legs and the plane perpendicular to the central axis of the dense phase section bed 3 is 20°. The outer diameter D of the spiral structure 螺外 =5.6mm(D) 螺外 / D 密内 =0.8); the pitch L1 of the spiral structure is 7mm (L1 / D) 密内 =1); The distance L2 between the internal component 5 and the gas distributor 2 is 7mm (L2 / D) 密内 =1); The height of the internal component 5 is H1 = 1.2m (H1 / H2 = 120%); and the cross-sectional area S1 of the main body 52 of the internal component is calculated to be S1 / S2 = 18.37% to the cross-sectional area S2 of the dense phase bed body 3;

[0081] The solid particles are glass microspheres, with a loading of 10g, a particle density of 2.378g / ml, a bulk density of 1.496g / ml, and an average particle size of 85.274μm as measured by a laser particle size analyzer, with a particle size distribution of 30-150μm; the fluidizing medium is air; and the operating conditions are room temperature and atmospheric pressure.

[0082] The fluidization state of the particles can be reflected by measuring the fluctuation of the bed pressure drop. If there is slugging, the bed pressure drop will fluctuate greatly. If there is no slugging, the bed pressure drop will fluctuate less, indicating that the fluidization is more uniform. In operation, a high-frequency differential pressure gauge is used to measure the particle bed pressure drop data in real time.

[0083] With an apparent gas velocity of 0.1 m / s, the height of the catalyst bed in the dense phase section 3 is 406 mm (calculated, the equivalent diameter of the catalyst bed cross-section is 6.32 mm, and based on the aforementioned height of 406 mm in the dense phase section 3, the height-to-diameter ratio of the catalyst bed in the dense phase section 3 is 406 / 6.32 = 64.24 > 10); the change in bed pressure drop with sampling time is measured, and the variation pattern is as follows... Figure 5 As shown. Wherein, the equivalent diameter of the catalyst bed cross-section = [(inner diameter D of the dense phase section bed 3)]. 密内 ) 2 -(Outer diameter of the main body of the internal component 52) 2 ] 1 / 2 .

[0084] according to Figure 5The pressure drop across the bed ranges from 2.95 ± 0.10 kPa.

[0085] Example 2 (S2)

[0086] The only difference from Example 1 is:

[0087] With an apparent gas velocity of 0.2 m / s, the height of the catalyst bed in the dense phase section 3 is 670 mm (calculated, the equivalent diameter of the catalyst bed cross-section is 6.32 mm, and based on the aforementioned height of 670 mm in the dense phase section 3, the height-to-diameter ratio of the catalyst bed in the dense phase section 3 is 670 / 6.32 = 106.01 > 10); the change in bed pressure drop with sampling time is measured, and the variation pattern is as follows... Figure 6 As shown.

[0088] according to Figure 6 The pressure drop across the bed ranges from 2.93 ± 0.12 kPa.

[0089] Comparative Example 1 (D1)

[0090] The only difference from Example 1 is:

[0091] No internal components 5;

[0092] With an apparent gas velocity of 0.1 m / s, the change in bed pressure drop over sampling time was measured, and the variation pattern is as follows: Figure 7 As shown.

[0093] according to Figure 7 The pressure drop across the bed ranges from 2.50 ± 0.19 kPa.

[0094] Comparative Example 2 (D2)

[0095] The only difference from Example 1 is:

[0096] No internal components 5;

[0097] With an apparent gas velocity of 0.2 m / s, the change in bed pressure drop over sampling time was measured, and the variation pattern is as follows: Figure 8 As shown.

[0098] according to Figure 8 The pressure drop across the bed ranges from 2.47 ± 0.46 kPa.

[0099] According to Example 1 and Comparative Example 1, and Figure 5 and Figure 7The comparison shows that, under the same conditions and with an apparent gas velocity of 0.1 m / s, compared with the gas-solid dense phase fluidized bed (D1) without internal component 5, the pressure drop fluctuation amplitude of the gas-solid dense phase fluidized bed (S1) with added internal component 5 is reduced, and decreases from 0.19 kPa to 0.10 kPa.

[0100] According to Example 2 and Comparative Example 2, and Figure 6 and Figure 8 The comparison shows that, under the same conditions and with an apparent gas velocity of 0.2 m / s, compared with the gas-solid dense phase fluidized bed (D2) without internal component 5, the pressure drop fluctuation amplitude of the gas-solid dense phase fluidized bed (S2) with added internal component 5 is reduced, and decreases from 0.46 kPa to 0.19 kPa.

[0101] Based on the above results and analysis, when using the gas-solid dense-phase fluidized bed of the present invention to fluidize solid particles, its internal components 5 can effectively break up large bubbles, significantly suppress the occurrence of slugging, improve fluidization quality, and reduce the fluctuation amplitude of bed pressure drop. Under the conditions of Example 1, the inner diameter D of the dense-phase bed 3 is... 密内 = 7mm, the height-to-diameter ratio of the catalyst bed is approximately 64; under the conditions of Example 2, the inner diameter D of the dense phase section bed 3 is... 密内 =7mm, the height-to-diameter ratio (height-to-diameter ratio = height of catalyst bed in dense phase section / equivalent diameter of cross section of dense phase section) is about 106; this shows that the dense phase fluidized bed device provided by the present invention can easily realize the operation of small inner diameter dense phase section bed and large height-to-diameter ratio catalyst bed.

Claims

1. An internal component for a gas-solid dense-phase fluidized bed, characterized in that, The gas-solid dense phase fluidized bed includes a bed body, a gas inlet (1), a gas distributor (2), a gas outlet (6), and a gas-solid separation device (7); the bed body includes a dense phase section bed body (3) from bottom to top and an expansion section bed body (4), the inner diameter of the expansion section bed body (4) being larger than the inner diameter of the dense phase section bed body (3); The internal components are coaxially disposed within the bed body; The internal components include a bubble-breaking structure (51), which is a spiral structure and is coaxially arranged with the bed body; the spiral structure is a continuous structure, including a linear spiral structure or a sheet spiral structure. The outer diameter D of the spiral structure 螺外 The inner diameter D of the dense phase section bed (3) 密内 The ratio D 螺外 / D 密内 =0.5-0.95; The pitch L1 of the spiral structure and the inner diameter D of the dense phase bed (3) 密内 The ratio L1 / D 密内 =0.5-2.

2. The internal component according to claim 1, characterized in that, The distance L2 between the internal component and the gas distributor (2) and the inner diameter D of the dense phase bed (3) 密内 The ratio L2 / D 密内 ≤3; and / or The ratio of the height H1 of the internal component to the height H2 of the dense phase section bed (3) is H1 / H2 ≥ 80%.

3. The internal component according to claim 1 or 2, characterized in that, The internal component also includes an internal component body (52), which is coaxially arranged with the bed body; The bubble-breaking structure (51) is disposed along the outer surface of the inner component body (52).

4. The internal component according to claim 3, characterized in that, The ratio of the cross-sectional area S1 of the main body (52) to the cross-sectional area S2 of the dense phase bed body (3) is 1-50%.

5. The internal component according to any one of claims 1, 2, and 4, characterized in that, The defoaming structure (51) is arranged along the inner wall of the dense phase bed (3).

6. A gas-solid dense-phase fluidized bed having internal components as described in any one of claims 1-5.

7. The gas-solid dense-phase fluidized bed according to claim 6, characterized in that, In the gas-solid dense phase fluidized bed, the height H2 of the dense phase section bed (3) and its inner diameter D 密内 The ratio H2 / D 密内 ≥3.

8. The gas-solid dense-phase fluidized bed according to claim 7, characterized in that, In the gas-solid dense-phase fluidized bed, the inner diameter D of the dense-phase section bed (3) is... 密内 ≤150 mm, catalyst bed height-to-diameter ratio >10.

9. A fluidization method for dense-phase fluidization of solid particles using a gas-solid dense-phase fluidized bed as described in any one of claims 6-8.

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