Air inlet distributor structure for hydrocyanic acid fluidized bed reactor

Abstract

The utility model relates to an air inlet distributor structure for a hydrocyanic acid fluidized bed reactor. The air inlet distributor structure comprises a plate-type distributor arranged at the bottom of the fluidized bed reactor, the conical sealing head is connected with the bottom of the fluidized bed reactor and defines an air pressure equalizing chamber; the air inlet pipe extends into the air pressure equalizing chamber from the side, an outlet of the air inlet pipe faces upwards, a guide plate with a conical umbrella surface is further arranged above the outlet end of the air inlet pipe, and a horizontal radial air guide port is formed between the bottom end of the guide plate and the outlet of the air inlet pipe. Compared with the prior art, the utility model can solve the problems of abrasion caused by direct washing of the plate-type distributor due to overlarge air flow in the air inlet pipe, poor catalyst accumulation or excessive abrasion caused by uneven air flow distribution and the like.

Description

TECHNICAL FIELD

[0001] The utility model belongs to fluidized bed reactor air distributor technical field relates to a kind of air inlet distributor structure for hydrogen cyanide fluidized bed reactor. BACKGROUND

[0002] The air inlet of hydrogen cyanide fluidized bed reactor is the core interface for realizing raw gas delivery and reaction environment regulation. After air enters the reactor through the inlet pipe, it needs to form a uniformly distributed gas-solid flow field to provide oxidant for the hydrogen cyanide synthesis reaction, and at the same time, through the disturbance of air flow, the catalyst particles are in a fluidized state, ensuring the full contact of reactants and catalysts.

[0003] The design structure at the air inlet pipe will directly affect the reaction efficiency and equipment safety:

[0004] (1) Unreasonable design of inlet pipe structure can cause air flow to directly hit the reactor wall, causing local wear;

[0005] (2) If the air is not evenly distributed after entering the reactor, the air flow velocity in some areas is too high, and the air flow velocity in some areas is too low, which can cause poor catalyst fluidization and catalyst accumulation, affecting the reaction efficiency;

[0006] (3) Local overheating caused by uneven air distribution (may cause catalyst deactivation) or incomplete reaction (reduce yield).

[0007] For example, the air inlet distributor structure of the fluidized bed reactor for producing hydrogen cyanide provided in Chinese patent CN119926305A includes an air pressure drop distributor, an air pressure equalization chamber, an air inlet pipe, and a deflector. The air inlet pipe of this patent admits air from the side, and although the deflector improves the air distribution effect to some extent, the baffle can only guide a small part of the air above the inlet, and the remaining air is freely distributed at their respective speeds after entering the air pressure equalization chamber, which cannot guarantee uniformity when entering the reactor.

[0008] In addition, the existing air inlet pipe often adopts a downward-facing flared mouth design, which can also solve the problems of catalyst accumulation and direct scouring of the distribution plate to some extent. However, due to the large diameter of the air inlet pipe, the air flow will be blocked by the inwardly extending air inlet pipe during the upward return process, resulting in uneven radial distribution. UTILITY MODEL CONTENTS

[0009] The utility model aims to provide an air inlet distributor structure for a hydrogen cyanide fluidized bed reactor to solve the problems of wear caused by excessive air flow directly scouring the plate-type distributor and poor catalyst accumulation or excessive wear caused by uneven air distribution.

[0010] The utility model discloses a purpose can be realized through the following technical scheme:

[0011] An air inlet distributor structure for a hydrogen cyanide fluidized bed reactor, comprising:

[0012] The plate distributor is arranged at the bottom of the fluidized bed reactor.

[0013] The conical head is connected with the bottom of the fluidized bed reactor and surrounds an air equalization chamber.

[0014] The air inlet pipe extends into the air equalization chamber from the side and has an upward outlet, and a conical umbrella-shaped guide plate is arranged above the outlet end of the air inlet pipe, and a horizontal radial air guide is formed between the bottom end of the guide plate and the outlet of the air inlet pipe.

[0015] Further, the outlet end of the air inlet pipe is located in the middle of the air equalization chamber.

[0016] Further, the taper angle of the guide plate is 30-60°.

[0017] Further, the distance H between the bottom end of the guide plate and the plate distributor satisfies H / D≥0.08-0.3, wherein D is the diameter of the bottom of the fluidized bed reactor.

[0018] Further, the taper of the conical head is θ=45°.

[0019] Further, the guide plate is connected with the air inlet pipe through a plurality of rib plates, and the radial air guides are formed between adjacent rib plates.

[0020] Further, the rib plates are arranged uniformly and spaced apart around the central axis of the outlet end of the air inlet pipe.

[0021] Further, the rib plates are welded at both ends to the outlet end of the air inlet pipe and the guide plate.

[0022] Further, the surface of the guide plate is polished to Ra≤3.2μm.

[0023] Compared with the prior art, the utility model has the following advantages:

[0024] (1) By arranging the air inlet pipe in the middle of the air equalization chamber and upward, and arranging the conical guide plate, the entering air can be effectively guided to be evenly distributed radially from the middle to the outer edge, avoiding the entering air flow directly hitting the plate distributor, and effectively realizing the uniform distribution of air.

[0025] (2) The guide plate adopts a specific guide angle, can effectively guide the airflow flow direction in cooperation with the rib plate, first collides downward at a certain angle, and then flows upward to the plate type distributor, so that more space is provided for mixing, and the pressure drop and distribution uniformity are effectively balanced.

[0026] (3) The guide plate adopts a conical shape, the conical angle of which is greater than the rest angle of the catalyst of the hydrogen cyanide fluidized bed reactor, and meanwhile, the conical surface is also polished, which can reduce the accumulation and retention of catalyst particles on the upper portion thereof. BRIEF DESCRIPTION OF DRAWINGS

[0027] Figure 1 It is a schematic view of the air inlet distributor structure of the utility model;

[0028] Marking description in the drawing:

[0029] 1-fluidized bed reactor, 2-plate type distributor, 3-air pressure equalizing chamber, 4-conical head, 5-guide plate, 6-rib plate, 7-air inlet pipe. DETAILED DESCRIPTION

[0030] The utility model will be described in detail below in combination with the drawings and specific embodiments. The embodiments are implemented on the premise of the technical scheme of the utility model, and detailed implementation modes and specific operation processes are given, but the protection scope of the utility model is not limited to the following embodiments.

[0031] In the description of the utility model, it should be explained that the orientation or position relationship indicated by the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer" and the like is based on the orientation or position relationship shown in the drawing, and is only for the convenience of describing the utility model and simplifying the description, and therefore cannot be understood as limiting the utility model. The indicated device or element must have a specific orientation, a specific orientation and operation, and therefore cannot be understood as limiting the utility model. In addition, the terms "first", "second", "third" are only for the purpose of description, and cannot be understood as indicating or implying relative importance.

[0032] In the description of the utility model, it should be explained that, unless otherwise explicitly specified and limited, the terms "mounting", "connection", "connection" should be understood broadly, for example, it can be fixedly connected, or it can be detachably connected, or integrally connected; it can be mechanically connected, or it can be electrically connected; it can be directly connected, or it can be indirectly connected through an intermediate medium; it can be the communication between two elements. For ordinary skilled in the art, the specific meaning of the above terms in the utility model can be understood according to the specific circumstances.

[0033] In the following embodiments or examples, if no specific function components or structures are mentioned, it means that the conventional components or structures are used in the field to achieve the corresponding functions.

[0034] To solve the problems of air inlet pipe 7 airflow too large and directly washing the plate distributor 2, causing wear, and uneven airflow distribution, leading to poor catalyst accumulation or excessive wear, etc., the utility model provides an air inlet distributor structure for hydrocyanic acid fluidized bed reactor 1, please see Figure 1 As shown, comprising:

[0035] The plate distributor 2 is arranged at the bottom of the fluidized bed reactor 1.

[0036] The conical head 4 is connected to the bottom of the fluidized bed reactor 1 and surrounds the air equalization chamber 3.

[0037] And the air inlet pipe 7 extends into the air equalization chamber 3 from the side and the outlet is upward, and the guide plate 5 in the shape of a conical umbrella is arranged above the outlet end of the air inlet pipe 7, and the bottom end of the guide plate 5 and the outlet of the air inlet pipe 7 form a horizontal radial air guide port.

[0038] In some specific embodiments, the outlet end of the air inlet pipe 7 is located in the middle of the air equalization chamber 3, so that the gas discharged from the outlet pipe of the air inlet pipe 7 can be uniformly dispersed from the center to the periphery, improving the uniformity of the air sent to the plate distributor 2. In addition, the plate distributor 2 here is used to uniformly distribute the air and other catalyst bed layers sent to the upper part, which is a commonly used distributor in the field, and the specific structure does not belong to the innovation protection point of the utility model, and will not be described here.

[0039] In some specific embodiments, the distance H between the bottom end of the guide plate 5 and the plate distributor 2 satisfies: H / D≥0.08~0.3, wherein D is the diameter of the bottom of the fluidized bed reactor 1. By limiting H within a suitable range, sufficient space can be provided for gas distribution, so that the gas can fully penetrate and disperse to be uniform before reaching the plate distributor 2, ensuring the stability of the hydrocyanic acid fluidized bed reactor 1 in the initial stage of fluidization. Here, if the value of H / D is too small, the radial diffusion distance of the gas flow will be long, affecting the uniformity of the edge area, and if the value of H / D is too large, the pressure drop will be too low, and the air supply effect of the plate distributor 2 will be reduced.

[0040] In some specific embodiments, the taper angle a of the guide plate 5 is 30-60°, and should be greater than the catalyst angle of repose. In addition, through research, it is found that in order to achieve sufficient gas distribution effect, the taper angle a of the guide plate 5 should be controlled to be about equal to arctan (k2D / H), wherein k2 is a coverage coefficient, which is usually less than 0.5, and in the present application, the value range is 0.25-0.45, preferably 0.3-0.38. Based on the relationship, it can be known that under the condition of fixed D, the larger H (the more sufficient development space), the smaller a required; on the contrary, if H is small, a larger a is required to achieve sufficient radial guiding effect.

[0041] In some specific embodiments, the taper of the conical head 4 is θ=45°, which satisfies the angle of repose of the catalyst used in the hydrocyanic acid fluidized bed reactor 1, but should not be too large to increase the equipment height and cost, etc.

[0042] In some specific embodiments, the guide plate 5 is connected with the air inlet pipe 7 through a plurality of rib plates 6, and the radial air guide openings are formed between adjacent rib plates 6. Here, the thickness of the rib plate 6 should not be too thick, and only the strength and other requirements are met.

[0043] In more specific embodiments, the rib plate 6 is provided with at least four plates, for example, 4, 5 and 6 plates, etc., and is uniformly and spacedly arranged around the central axis of the outlet end of the air inlet pipe 7.

[0044] In more specific embodiments, the rib plate 6 is welded and connected between the outlet end of the air inlet pipe 7 and the guide plate 5.

[0045] In some specific embodiments, the surface of the guide plate 5 is also subjected to polishing treatment, so that Ra≤3.2μm.

[0046] The above embodiments can be implemented individually, or any two or more combinations can be implemented without violating the logic.

[0047] The above embodiments will be described in more detail below in combination with specific examples.

[0048] Example 1:

[0049] In order to solve the problems of excessive air flow of the air inlet pipe 7 directly washing the plate distributor 2 to cause abrasion, and uneven gas flow distribution to cause poor accumulation or excessive abrasion of the catalyst, etc., the present embodiment provides an air inlet distributor structure for a hydrocyanic acid fluidized bed reactor 1, please refer to Figure 1 as shown, which comprises:

[0050] The plate distributor 2 arranged at the bottom of the fluidized bed reactor 1;

[0051] A conical head 4 connected with the bottom of the fluidized bed reactor 1 and surrounding an air equalization chamber 3;

[0052] An air inlet pipe 7 extending into the air equalization chamber 3 from the side and having an outlet upward, and a conical umbrella-shaped guide plate 5 is further arranged above the outlet end of the air inlet pipe 7, and a horizontal radial air guide is formed between the bottom end of the guide plate 5 and the outlet of the air inlet pipe 7.

[0053] Please refer to Figure 1 It is shown that the outlet end of the air inlet pipe 7 is located in the middle of the air equalization chamber 3, so that the gas discharged from the outlet pipe of the air inlet pipe 7 can be uniformly dispersed from the center to the periphery, improving the uniformity of the air sent to the plate distributor 2.

[0054] Please refer to Figure 1 It is shown that the spacing H between the bottom end of the guide plate 5 and the plate distributor 2 satisfies: H / D≥0.08~0.3, wherein D is the diameter of the bottom of the fluidized bed reactor 1, by limiting H in a suitable range, sufficient space can be provided for gas distribution, so that the gas can be fully penetrated and dispersed to be uniform before reaching the plate distributor 2, and the stability of the hydrocyanic acid fluidized bed reactor 1 in the initial stage of fluidization is ensured. Here, if the value of H / D is too small, the radial diffusion distance of the gas flow will be long, which will affect the uniformity of the edge area, and if the value of H / D is too large, the pressure drop will be too low, which will reduce the air supplement effect of the plate distributor 2.

[0055] Please refer to Figure 1 It is shown that the taper angle α of the guide plate 5 is 30~60°, and through research it is found that in order to achieve sufficient gas distribution effect, the taper angle α of the guide plate 5 should be controlled to be about equal to arctan(k2·D / H), wherein k2 is a coverage coefficient, which is usually less than 0.5, and in the present application, the value range is 0.25~0.45, preferably 0.3~0.38, based on the relationship, under the fixed D, the larger H (development space) is, the smaller α required can be; on the contrary, if H is small, a larger α is required to achieve sufficient radial guiding effect.

[0056] Please refer to Figure 1 It is shown that the taper θ of the conical head 4 is 45°, which satisfies the rest angle of the catalyst used in the hydrocyanic acid fluidized bed reactor 1, but it is not too large to increase the equipment height and cost.

[0057] The guide plate 5 is connected with the air inlet pipe 7 through a plurality of webs 6, and the radial air inlets are formed between adjacent webs 6. The thickness of the web 6 is not too thick, and the strength and other requirements are met. The web 6 is provided with at least four webs, for example, 4, 5 and 6, and is uniformly and spacedly arranged around the central axis of the outlet end of the air inlet pipe 7. The two ends of the web 6 are respectively welded and connected between the outlet end of the air inlet pipe 7 and the guide plate 5.

[0058] The surface of the guide plate 5 is also polished to Ra≤3.2μm, which can effectively reduce the accumulation of catalyst particles on the upper part of the guide plate 5.

[0059] The air inlet distributor structure of the embodiment can effectively avoid the vortex or dead zone formed after the air flow is introduced, avoid the wear of the reactor caused by air flow impact, avoid the excessive wear or local reaction of the catalyst caused by the local flow rate being too high, and also prevent the catalyst from settling and the reaction efficiency from being reduced caused by the flow rate being too low, so as to ensure the full fluidization of the catalyst and improve the fluidization effect of the catalyst, thereby improving the reaction efficiency.

[0060] At the same time, the conical guide plate 5 effectively avoids the accumulation of catalyst particles and reduces the cleaning and maintenance cost. The welding connection enhances the stability of the connection and ensures the safe operation of the equipment.

[0061] In summary, the adaptive air inlet layout of the embodiment solves the problems of local wear of the reactor wall caused by the straight impact of the air inlet pipe 7, uneven air flow distribution (vortex / dead zone) caused by the lack of guide, and accumulation or excessive wear of the catalyst caused by poor fluidization. At the same time of ensuring the uniform distribution of air in the reactor, the construction convenience and structural reliability are improved. Through the precise design of the angle and spacing of the conical guide plate 5, the optimization of the conical surface to prevent material accumulation, and the welding integrated connection, the reaction efficiency and equipment safety are ensured, the service life of the reactor is prolonged, and reliable protection is provided for the long-term stable operation of the hydrocyanic acid fluidized bed reactor 1.

[0062] The above description of the embodiments is for the convenience of those skilled in the art to understand and use the utility model. Those skilled in the art can easily make various modifications to these embodiments, and apply the general principles described herein to other embodiments without creative labor. Therefore, the utility model is not limited to the above embodiments, and the improvements and modifications made by those skilled in the art without departing from the scope of the utility model should be within the protection scope of the utility model.

Claims

1. An air inlet distributor structure for a hydrocyanic acid fluidized bed reactor, characterized by, The application relates to a fluidized bed reactor, comprising: a plate distributor arranged at the bottom of the fluidized bed reactor; a conical head connected to the bottom of the fluidized bed reactor and surrounding an air equalizing chamber; an air inlet pipe extending into the air equalizing chamber from the side and having an upward outlet, and a conical umbrella-shaped guide plate arranged above the outlet end of the air inlet pipe, wherein a horizontal radial air guide is formed between the bottom end of the guide plate and the outlet of the air inlet pipe.

2. An air inlet distributor structure for a hydrocyanic acid fluidized bed reactor according to claim 1, characterized in that, The outlet end of the air inlet pipe is located in the middle of the air equalizing chamber.

3. An air inlet distributor structure for a hydrocyanic acid fluidized bed reactor according to claim 1, characterized in that, The conical angle alpha of the guide plate is 30-60 degrees.

4. An air inlet distributor structure for a hydrocyanic acid fluidized bed reactor according to claim 1, characterized in that, The distance H between the bottom end of the guide plate and the plate distributor satisfies the condition H / D=0.08-0.3, wherein D is the diameter of the bottom of the fluidized bed reactor.

5. An air inlet distributor structure for a hydrocyanic acid fluidized bed reactor according to claim 1, characterized in that, The conical angle theta of the conical head is 45 degrees.

6. An air inlet distributor structure for a hydrocyanic acid fluidized bed reactor according to claim 1, characterized in that, The guide plate is connected to the air inlet pipe through a plurality of rib plates, and the radial air guide is formed between adjacent rib plates.

7. An air inlet distributor structure for a hydrocyanic acid fluidized bed reactor according to claim 6, characterized in that, The rib plates are arranged around the central axis of the outlet end of the air inlet pipe in a uniform and spaced manner.

8. An air inlet distributor structure for a hydrocyanic acid fluidized bed reactor according to claim 6, characterized in that, The two ends of the rib plates are respectively welded to the outlet end of the air inlet pipe and the guide plate.

9. An air inlet distributor structure for a hydrocyanic acid fluidized bed reactor according to claim 1, characterized in that, The surface of the guide plate is also subjected to polishing treatment, and Ra<=3.2 microns.

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