Feed gas inlet distributor for hydrocyanic acid fluidized bed reactor

Abstract

The utility model relates to a feed gas inlet distributor for a hydrocyanic acid fluidized bed reactor, and belongs to the technical field of chemical equipment. The distributor comprises a low-stress inlet connecting pipe arranged on a reactor main body, and a premixing chamber and a feed gas distributor which are arranged in the reactor main body. And the low-stress inlet connecting pipe is used for introducing high-temperature raw material gas. The premixing chamber comprises at least one section of horizontal premixing chamber communicated with the inner connecting pipe and at least one section of vertical premixing chamber communicated with the horizontal premixing chamber, and is used for fully mixing high-temperature feed gas. The raw material gas distributor comprises an inlet main pipe, a horizontal branch pipe, a horizontal branch pipe and a nozzle, and is used for uniformly spraying preheated and premixed raw material gas into the reactor main body. Compared with the prior art, the feed gas inlet distributor disclosed by the utility model is suitable for high-temperature methanol and ammonia feed gas media, the operation performance of a hydrocyanic acid fluidized bed reactor can be remarkably improved, and a more efficient and stable solution is provided for industrial production of hydrocyanic acid.

Description

TECHNICAL FIELD

[0001] The utility model relates to a chemical equipment technical field especially is hydrogen cyanide fluidized bed reactor raw material gas import distributor. BACKGROUND

[0002] The raw material gas import distributor is a key component in the hydrogen cyanide reactor, and its performance directly affects the gas-solid contact efficiency, heat and mass transfer effect, reaction selectivity and operation stability in the reactor. The existing import distributor adopts the design of "multi-quadrant pipe connection inlet", which is usually used to directly introduce methanol and ammonia and other raw material gases into the gas distribution cavity below the distributor through multiple independent symmetrical pipelines.

[0003] However, even this seemingly symmetrical design, due to its environment (high temperature, high-speed airflow, catalyst particle abrasion, corrosive medium) and high requirements for mixing and uniform distribution, there are still the following problems in actual operation:

[0004] (1) uneven gas mixing and poor mixing effect: methanol and ammonia directly enter the distributor from the pipeline and cannot be fully mixed before entering the catalyst bed, which cannot ensure uniform fluidization of the entire bed, resulting in local overheating and local area methanol or ammonia concentration too high, affecting the reaction effect.

[0005] (2) thermal stress and mechanical fatigue: the reactor operating temperature is usually 400-500 DEG C, while the temperature of the entering methanol-ammonia mixture is relatively low. The huge temperature difference will cause huge thermal stress at the pipe connection inlet and the connection of the distribution plate. Especially in the start-stop condition, repeated temperature cycles will cause fatigue cracks in the weld and heat affected zone, causing leakage. The distributor pipeline or support may be deformed due to thermal stress, affecting its position and jet angle.

[0006] (3) reaction gas is not preheated: the methanol ammonia mixed gas is not preheated directly into the reactor, and the temperature difference and fluid dynamics of the reactor internal environment cause local temperature gradient and thermal shock, aggravating the thermal stress problem.

[0007] Therefore, in view of the above problems of methanol ammonia distributor in the hydrogen cyanide reactor, a new type of raw material gas import distributor needs to be developed. UTILITY MODEL CONTENT

[0008] The utility model discloses a raw material gas import distributor for hydrogen cyanide fluidized bed reactor, which overcomes the defects of the methanol ammonia distributor in the hydrogen cyanide reactor.

[0009] The purpose of the utility model can be realized by the following technical solutions:

[0010] The utility model provides a raw material gas inlet distributor for hydrocyanic acid fluidized bed reactor, including low stress inlet connecting pipe of being located on the reactor main body, and premixing chamber and raw material gas distributor of being located in the reactor main body,

[0011] The low stress inlet connecting pipe is used for passing in high temperature raw material gas, and specifically includes inner connecting pipe which is horizontally through the reactor main body and outer connecting pipe which is annularly arranged at the periphery of the connecting place of the inner connecting pipe and the reactor main body, and a thermal expansion space is formed between the outer connecting pipe and the outer wall of the inner connecting pipe,

[0012] The premixing chamber includes at least one horizontal premixing chamber which is communicated with the inner connecting pipe and at least one vertical premixing chamber which is communicated with the horizontal premixing chamber, and the horizontal premixing chamber and the vertical premixing chamber are both provided with mixing auxiliary parts in the axial direction for fully mixing the high temperature raw material gas,

[0013] The raw material gas distributor includes inlet main pipe, horizontal branch pipe, horizontal branch pipe and nozzle, the inlet main pipe is connected with the vertical premixing chamber, the horizontal branch pipe is connected with the inlet main pipe and extends towards the inner wall of the reactor main body, the horizontal branch pipe is connected with the horizontal branch pipe and extends towards the inner wall of the reactor main body, and the nozzle is spaced on the horizontal branch pipe and is used for uniformly spraying the preheated and premixed raw material gas into the reactor main body.

[0014] Further, the outer connecting pipe and the inner connecting pipe are connected through a flexible compensation connecting piece.

[0015] Still further, one end of the flexible compensation connecting piece is connected with the outer connecting pipe, and the other end of the flexible compensation connecting piece is inwardly retracted to be connected with the inner connecting pipe.

[0016] Further, the flexible compensation connecting piece includes a straight line segment and an arc connecting segment which are integrally connected.

[0017] Still further, the straight line segment is welded with the outer connecting pipe, and the arc connecting segment is welded with the inner connecting pipe.

[0018] Still further, the curvature radius of the arc connecting segment is 10-20mm.

[0019] Further, the width of the thermal expansion space is 20-40mm.

[0020] Further, the number of the horizontal premixing chambers is 3-5.

[0021] Further, the number of the vertical premixing chambers is 5-10.

[0022] Still further, the first horizontal premixing chamber is communicated with the inner connecting pipe of the low stress inlet connecting pipe, and the remaining horizontal premixing chambers are connected in sequence.

[0023] Further, the first vertical premixing chamber is communicated with the tail horizontal premixing chamber through the through arc transition section; the remaining vertical premixing chambers are connected in sequence; and the tail vertical premixing chamber is communicated with the raw material gas distributor.

[0024] Further, the volume of the horizontal premixing chamber and the vertical premixing chamber is 0.5-3m 3 .

[0025] Further, the length of the single section of the mixing auxiliary part is 0.5-3m.

[0026] Further, a gap of 0.1-0.3m is left between the mixing auxiliary parts in the adjacent horizontal premixing chambers or the adjacent vertical premixing chambers.

[0027] Further, the mixing auxiliary part is any one or a combination of the mixing device and the axial fin.

[0028] Further, the mixing device is any one or more of the static baffle type, the orifice plate type and the tee type mixing device.

[0029] Further, the axial fin is any one or more of the straight fin, the spiral plate fin and the corrugated plate fin.

[0030] Further, when the straight fin is selected as the axial fin, the straight fins are uniformly arranged along the inner wall of the horizontal premixing chamber or the vertical premixing chamber.

[0031] Further, the straight fins in the adjacent horizontal premixing chambers or the adjacent vertical premixing chambers are distributed at staggered angles.

[0032] Further, the distribution area of the nozzle is divided into A zone, B zone and C zone.

[0033] Further, the A zone is located in the area of 25%-40% of the length of the horizontal branch pipe, the B zone is located in the area of 20%-30% of the middle of the length of the horizontal branch pipe, and the C zone is located in the area of 25%-35% of the rear of the length of the horizontal branch pipe.

[0034] Further, the nozzle aperture of the A zone is 5-6.5mm.

[0035] Further, the nozzle aperture of the B zone and the C zone is increased by 0.1-0.3mm in each zone.

[0036] Compared with the prior art, the utility model has the following technical advantages:

[0037] (1) The raw material gas inlet distributor for the hydrocyanic acid fluidized bed reactor of the utility model ingeniously optimizes the structural setting of the inlet connecting pipe and the reactor main body connection, effectively absorbs the thermal expansion and shrinkage caused by temperature change, and is suitable for the import of preheated high-temperature methanol ammonia raw material gas. In addition, the utility model innovatively sets a relatively large space as a premixing chamber before the methanol and ammonia enter the distributor nozzle, for the full mixing of methanol and ammonia; finally, the methanol ammonia raw material gas after preheating and premixing is uniformly injected into the reactor main body through the raw material gas distributor, realizing the efficient import and injection of methanol ammonia raw material gas. Through the synergistic effect of the above technical improvements, the novel raw material gas inlet distributor of the utility model can significantly improve the operation performance of the hydrocyanic acid fluidized bed reactor, especially suitable for the import and distribution of high-temperature methanol ammonia raw material gas, providing a more efficient, more stable and safer solution for the industrial production of hydrocyanic acid.

[0038] (2) The premixing chamber of the utility model can select mixers, fins and other mixing devices according to actual needs to enhance gas mixing efficiency and improve fluid dynamics characteristics, so as to ensure that the methanol and ammonia entering the reactor can be fully and uniformly mixed, and enter the catalyst bed layer in an ideal flow pattern.

[0039] (3) The utility model innovatively specifically divides the distribution area of the distributor nozzle, and differentiates the aperture size of the nozzles in different partitions according to the distance between the nozzle and the horizontal branch pipe and the gas amount required by each area. Specifically, smaller aperture nozzles are used in the area close to the horizontal branch pipe, while larger aperture nozzles are used in the area far away, to compensate for the resistance loss along the way and ensure that the gas flow rate and flow of each zone outlet are uniform. This fine partition design can effectively avoid the problem of local overheating or low reaction efficiency caused by uneven gas distribution of traditional distributors, thereby improving the overall performance and product yield of the reactor. BRIEF DESCRIPTION OF DRAWINGS

[0040] Figure 1 It is the overall structure schematic view of the raw material gas inlet distributor of the utility model.

[0041] Figure 2 It is the structure schematic view of the low-stress inlet connecting pipe of the utility model.

[0042] Figure 3 It is the structure schematic view of the mixer in the premixing chamber of the utility model.

[0043] Figure 4 It is the structure schematic view of the straight fin in the premixing chamber of the utility model.

[0044] Figure 5 It is the structure schematic view of the corrugated fin in the premixing chamber of the utility model.

[0045] Figure 6 The utility model discloses a raw material gas distributor's structural schematic diagram.

[0046] Marked explanation in the drawing:

[0047] 1-reactor main body;

[0048] 2-low stress inlet connector, 21-inner connector, 22-outer connector, 23-thermal expansion space, 24-flexible compensation connecting piece, 241-linear segment, 242-arc connecting segment;

[0049] 3-premixing chamber, 31-horizontal premixing chamber, 32-vertical premixing chamber, 33-mixer, 34-axial fin, 35-arc transition section;

[0050] 4-raw material gas distributor, 41-inlet main pipe, 42-horizontal branch pipe, 43-horizontal branch pipe, 44-nozzle. DETAILED DESCRIPTION

[0051] The utility model will be explained in detail below in combination with the drawings and specific embodiment. The embodiment is implemented with the utility model technical scheme as the premise, gives detailed implementation mode and specific operation process, but the protection scope of the utility model is not limited to the following embodiment.

[0052] In the utility model, it needs to be explained that the orientation or position relation indicated by the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer" and the like is based on the orientation or position relation shown in the drawing, and is only for the convenience of describing the utility model and simplifying the description, and does not indicate or imply that the indicated device or element must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as a limitation on the utility model; the terms "first", "second", "third" are only for the purpose of description, and cannot be understood as indicating or implying relative importance; in addition, unless otherwise explicitly specified and limited, the terms "mounting", "connecting", "connecting" should be understood broadly, for example, can be fixedly connected, can be detachably connected, or integrally connected;It can be mechanical connection, or electrical connection;It can be direct connection, or indirect connection through intermediate medium, it can be the communication inside 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.

[0053] It should be noted that: similar signs and letters represent similar items in the following drawings, therefore, once an item is defined in one drawing, it does not need to be further defined and explained in the subsequent drawings.

[0054] The raw material gas inlet distributor for the existing hydrocyanic acid fluidized bed reactor often uses multiple independent symmetrical pipelines to directly introduce methanol and ammonia and other raw material gases into a gas distribution chamber below the distributor. However, the following problems still exist in actual operation: (1) uneven and poor mixing of gases; (2) thermal stress and mechanical fatigue; (3) unpreheated reaction gas; (4) complex control system and inconsistent response.

[0055] Based on this, the utility model provides a kind of raw material gas inlet distributor for the hydrocyanic acid fluidized bed reactor. As shown in Figure 1 The raw material gas inlet distributor specifically includes low-stress inlet connecting pipe 2 arranged on reactor main body 1, and premixing chamber 3 and raw material gas distributor 4 arranged in reactor main body 1.

[0056] As shown in Figure 2 The low-stress inlet connecting pipe 2 of the utility model is used to pass high-temperature raw material gas, and specifically includes inner connecting pipe 21 horizontally penetrating reactor main body 1 and outer connecting pipe 22 annularly arranged at the outer periphery of the connection between inner connecting pipe 21 and reactor main body 1, and thermal expansion space 23 is formed between outer connecting pipe 22 and the outer wall of inner connecting pipe 21.

[0057] As shown in Figure 1 The premixing chamber 3 of the utility model includes at least one horizontal premixing chamber 31 in communication with inner connecting pipe 21, and at least one vertical premixing chamber 32 in communication with horizontal premixing chamber 31. Mixing auxiliary parts are arranged in horizontal premixing chamber 31 and vertical premixing chamber 32 along the axial direction, for fully mixing high-temperature raw material gas.

[0058] As shown in Figure 6 The raw material gas distributor 4 of the utility model includes inlet main pipe 41, horizontal branch pipe 42, horizontal branch pipe 43 and nozzle 44, inlet main pipe 41 is connected with vertical premixing chamber 32, horizontal branch pipe 42 is connected with inlet main pipe 41 and extends towards the inner wall of reactor main body 1, horizontal branch pipe 43 is connected with horizontal branch pipe 42 and extends towards the inner wall of reactor main body 1. Nozzle 44 is arranged on horizontal branch pipe 43, for uniformly injecting preheated and premixed raw material gas into reactor main body 1.

[0059] In some specific embodiments, the outer connecting pipe 22 and the inner connecting pipe 21 are connected through a flexible compensation connecting piece 24. One end of the flexible compensation connecting piece 24 is connected with the outer connecting pipe 22, and the other end of the flexible compensation connecting piece 24 is inwardly retracted to be connected with the inner connecting pipe 21.

[0060] In some more specific embodiments, the flexible compensation connecting piece 24 includes linear segment 241 and arc-shaped connecting segment 242 connected integrally. The linear segment 241 is welded with the outer connecting pipe 22, and the arc-shaped connecting segment 242 is welded with the inner connecting pipe 21.

[0061] In some more specific embodiments, the curvature radius of the arc-shaped connecting section 242 is 10-20 mm.

[0062] In some specific embodiments, the width of the thermal expansion space 23 is 20-40 mm.

[0063] The utility model discloses a novel inlet structure which can reduce the thermal stress of the inlet connecting pipe, and by optimizing the structural setting of the connecting pipe and the reactor main body connecting place and / or using the connecting piece with flexible compensation capacity, effectively absorbing the thermal expansion and contraction caused by temperature change, thereby significantly reducing the thermal stress concentration of the connecting position, avoiding the mechanical fatigue and crack caused by the traditional rigid connection, and improving the operation safety.

[0064] In some specific embodiments, the number of the horizontal premixing chambers 31 is 3-5.

[0065] In some specific embodiments, the number of the vertical premixing chambers 32 is 5-10.

[0066] In some more specific embodiments, the first horizontal premixing chamber 31 is communicated with the inner connecting pipe 21 of the low-stress inlet connecting pipe 2, and the remaining horizontal premixing chambers 31 are connected in sequence.

[0067] In some more specific embodiments, the first vertical premixing chamber 32 is communicated with the last horizontal premixing chamber 31 through the through arc-shaped transition section 35, and the remaining vertical premixing chambers 32 are connected in sequence, and the last vertical premixing chamber 32 is communicated with the raw material gas distributor 4.

[0068] In some specific embodiments, the volume of the horizontal premixing chamber 31 and the vertical premixing chamber 32 is 0.5-3 m 3 .

[0069] In some specific embodiments, the length of the single section of the mixing auxiliary part is 0.5-3 m.

[0070] In some specific embodiments, a gap of 0.1-0.3 m is left between the mixing auxiliary parts in the adjacent horizontal premixing chambers 31 or the adjacent vertical premixing chambers 32.

[0071] In the production process of hydrogen cyanide, the methanol ammonia feed distributor is long-term in high temperature. When the temperature of the mixed gas is higher than the temperature of ammonia decomposing active nitrogen atom, part of ammonia will decompose active nitrogen atom, and combine with metal atom in the feed distributor pipe, produce brittle metal nitride, cause the rupture of the feed distributor. Therefore, the utility model innovatively sets up a relatively larger space as a premixing chamber before methanol and ammonia enter the distributor nozzle, for the preliminary mixing of methanol and ammonia. Methanol and ammonia gas first enter the premixing chamber through the inlet pipeline, and then are further mixed in the premixing chamber. The volume and geometric shape of the premixing chamber are optimized and designed, which can effectively ensure that methanol and ammonia gas have sufficient residence time and turbulence degree in the space to realize sufficient mixing.

[0072] As Figures 3-5 Indicated, in some specific embodiments, the mixing aid is any one or a combination of the mixer 33, the axial fin 34.

[0073] In some specific embodiments, the mixer 33 is any one or more of a static baffle type, a perforated plate type, a tee type mixer.

[0074] In some specific embodiments, the axial fin 34 is any one or more of a straight fin, a spiral plate fin or a corrugated plate fin.

[0075] In some more specific embodiments, when the axial fin 34 is selected as a straight fin, the straight fin is uniformly arranged along the inner wall of the horizontal premixing chamber 31 or the vertical premixing chamber 32 in a ring shape. The straight fins in adjacent horizontal premixing chambers 31 or vertical premixing chambers 32 are distributed at staggered angles.

[0076] In some more specific embodiments, the thickness of the axial fin 34 is 6-10mm.

[0077] The premixing chamber of the utility model is internally designed with a variety of optional mixing aids, such as fin structures (straight / corrugated) or mixer structures. The main purpose of setting the fins and / or mixers is to enhance the gas mixing efficiency and improve the fluid dynamics characteristics, so as to ensure that the methanol and ammonia entering the reactor can be fully and uniformly mixed, and enter the catalyst bed layer in an ideal flow pattern.

[0078] Specifically, the fin structure arranged in the premixing chamber mainly has the following functions and effects: (1) enhancing gas mixing: the fins can disturb the laminar flow state of the gas and force the gas to generate strong turbulent flow. The turbulent flow can significantly increase the contact area and diffusion rate between different gas components, thereby achieving rapid and uniform mixing in a short distance. In addition, shear force is generated when the gas flows through the fins, which helps to break up gas clumps and promote mixing at the molecular level. Furthermore, the arrangement of fins can divide a large gas flow into multiple small gas flows, and then the multiple small gas flows are recombined between every two fins, and then the recombined gas flows are again divided through the fins with staggered angles. The repeated process of division-recombination-again division can effectively promote mixing. (2) improving fluid distribution and flow pattern: in the long pipeline of the premixing chamber, the radial velocity of the gas flow may not be uniform, such as high central velocity and low wall velocity. The fins can help to improve the radial velocity distribution and make the gas flow more uniform in the pipeline cross section. In addition, if the bend connection between the upstream pipeline or the horizontal premixing chamber and the vertical premixing chamber causes vortex flow of the gas flow, the fins can act as a fairing or a guide vane to eliminate or weaken the rotational flow, so that the gas flow flows along the axial direction, which is beneficial to ensure the uniformity of the subsequent entering into the distribution plate or the catalyst bed. (3) improving the stability of the reactor operation: by ensuring that the mixed gas entering the reactor is uniform and has a good flow pattern, the local fluctuations in the reactor can be reduced, which helps to maintain the stable fluidization state of the catalyst bed and avoid channeling or dead zones, thereby improving the overall operation stability of the reactor.

[0079] As shown in Figure 6 In some specific embodiments, the distribution area of the nozzle 44 is divided into A, B and C zones.

[0080] In some more specific embodiments, the A zone is located in the front 25%-40% of the length of the horizontal branch pipe 43, the B zone is located in the middle 20%-30% of the length of the horizontal branch pipe 43, and the C zone is located in the rear 25%-35% of the length of the horizontal branch pipe 43.

[0081] In some more specific embodiments, the aperture of the nozzle 44 in the A zone is 5-6.5 mm.

[0082] In some more specific embodiments, the aperture of the nozzle 44 in the B and C zones increases by 0.1-0.3 mm per zone.

[0083] This invention innovatively divides the distribution area of ​​the distributor nozzles into specific zones and differentiates the nozzle orifice size of different zones based on the distance between the nozzles and the inlet main pipe 41 / horizontal branch pipe 42 and the required gas volume of each zone. Specifically, the zone closer to the inlet main pipe 41 / horizontal branch pipe 42 (i.e., zone A) uses nozzles with smaller orifice diameters, while the zones farther away (such as zones B / C) use nozzles with larger orifice diameters to compensate for friction loss and ensure uniform gas velocity and flow rate at the outlet of each zone. This refined zone design effectively avoids the problems of local overheating or low reaction efficiency caused by uneven airflow distribution in traditional distributors, thereby improving the overall performance of the reactor and product yield.

[0084] Each of the above embodiments can be implemented individually, or in any combination of two or more. The following detailed description of specific examples will further illustrate these embodiments.

[0085] Example 1:

[0086] This embodiment provides a feed gas inlet distributor for a hydrogen cyanide fluidized bed reactor. For example... Figure 1 As shown, the feed gas inlet distributor specifically includes a low-stress inlet pipe 2 installed on the reactor body 1, and a premixing chamber 3 and a feed gas distributor 4 installed inside the reactor body 1.

[0087] like Figure 2 As shown, the low-stress inlet pipe 2 in this embodiment is used to introduce high-temperature raw material mixture gas. Specifically, it includes an inner pipe 21 that horizontally penetrates the reactor body 1 and an outer pipe 22 surrounding the connection between the inner pipe 21 and the reactor body 1. The outer pipe 22 and the inner pipe 21 are connected by a flexible compensation connector 24. The flexible compensation connector 24 in this embodiment includes an integrally connected straight section 241 and an arc-shaped connecting section 242. The straight section 241 of the flexible compensation connector 24 is welded to the outer pipe 22, and the radius of curvature of the arc-shaped connecting section 242 is approximately 15 mm. The arc-shaped connecting section 242 tapers inward to weld to the inner pipe 21, creating a thermal expansion space 23 with a width of approximately 30 mm between the outer walls of the outer pipe 22 and the inner pipe 21. This effectively absorbs thermal expansion and contraction caused by temperature changes, significantly reducing thermal stress concentration at the connection point, avoiding mechanical fatigue and cracks that may occur with traditional rigid connections, and improving operational safety.

[0088] In this embodiment, the premixing chamber 3 includes four horizontal premixing chambers 31 and eight vertical premixing chambers 32. The volume of both the horizontal premixing chambers 31 and the vertical premixing chambers 32 is 2m³. 3The first horizontal premixing chamber 31 is communicated with the inner connecting pipe 21, and the remaining horizontal premixing chambers 31 are sequentially connected and fluidly communicated. The first vertical premixing chamber 32 is communicated with the tail horizontal premixing chamber 31 through the through arc transition section 35, and the remaining vertical premixing chambers 32 are sequentially connected and fluidly communicated, and the tail vertical premixing chamber 32 is communicated with the raw material gas distributor 4. Thus, the raw material gas of high temperature methanol ammonia is smoothly introduced through the communication of the inner connecting pipe 21 of the low stress inlet connecting pipe 2, the horizontal premixing chamber 31, the vertical premixing chamber 32 and the raw material gas distributor 4.

[0089] The horizontal premixing chamber 31 and the vertical premixing chamber 32 of the embodiment are each provided with a mixing auxiliary element in the axial direction, which is any one or a combination of the mixers 33 and the axial fins 34, that is, each of the horizontal premixing chamber 31 or the vertical premixing chamber 32 can be a mixer alone, a fin alone or a combination of the two. The single section length of the mixing auxiliary element is 0.5-3 m, and a gap of 0.1-0.3 m is left between the mixing auxiliary elements in adjacent horizontal premixing chambers 31 or adjacent vertical premixing chambers 32.

[0090] As shown in Figure 3 , the mixer 33 of the embodiment is any one or more of the static baffle type, the orifice plate type and the tee type mixer, for example, the static baffle type mixer can be selected.

[0091] As shown in Figure 4 , the axial fin 34 of the embodiment selects a straight fin, which is uniformly arranged along the inner wall of the horizontal premixing chamber 31 or the vertical premixing chamber 32, and the straight fins in adjacent horizontal premixing chambers 31 or vertical premixing chambers 32 (that is, the straight fins in the continuous two end premixing chambers) are distributed at an interlaced angle, and the interlaced angle is 15-30°, for example, 20°. The thickness of the axial fin 34 is 6-10 mm, for example, 6 mm.

[0092] As shown in Figure 6 , the raw material gas distributor 4 of the embodiment includes an inlet main pipe 41, a horizontal branch pipe 42, a horizontal sub-pipe 43 and a nozzle 44. The inlet main pipe 41 is connected with the vertical premixing chamber 32, the horizontal branch pipe 42 is connected with the inlet main pipe 41 and extends towards the inner wall of the reactor main body 1, the horizontal sub-pipe 43 is connected with the horizontal branch pipe 42 and extends towards the inner wall of the reactor main body 1, so that the horizontal branch pipe 42 and the horizontal sub-pipe 43 are arranged longitudinally and transversely to form a nozzle distribution area which is a "discoid". The nozzle 44 is arranged on the horizontal sub-pipe 43 and is used for uniformly spraying the preheated and premixed raw material gas into the reactor main body 1.

[0093] The distribution area of the nozzles 44 in this embodiment is divided into A, B and C zones. The A zone is located in the front 35% of the length of the horizontal branch pipe 43, the B zone is located in the middle 30% of the length of the horizontal branch pipe 43, and the C zone is located in the rear 35% of the length of the horizontal branch pipe 43. The nozzle 44 aperture in the A zone is 5.6 mm, the nozzle 44 aperture in the B zone is 5.8 mm, and the nozzle 44 aperture in the C zone is 6.1 mm. The number of nozzles 44 in the A, B and C zones is approximately equal, and the spacing between adjacent nozzles 44 is 180 mm.

[0094] The working principle of the raw gas inlet distributor for the hydrocyanic acid fluidized bed reactor in this embodiment is as follows:

[0095] (1) Raw material entry and pretreatment: High-purity methanol and ammonia are drawn from their respective storage tanks or supply systems. To ensure reaction efficiency and protect the catalyst, these raw materials are usually pretreated to remove potential impurities. At the same time, a large amount of air is compressed and fed into the system, and the air may also be filtered to remove dust and particulate matter.

[0096] (2) Preheating and initial mixing: After the main raw materials of methanol and ammonia enter the reactor through the low-stress inlet connection pipe 2, they are preheated and mixed in multiple premixing chambers 3 by mixers 33 and / or axial fins 34, so that they reach the initial temperature required for the reaction (usually between 350-450°C).

[0097] (3) Injection into the reactor: The preheated and mixed gas passes through the inlet main pipe 41 of the raw gas distributor 4, then flows through the horizontal branch pipe 42 and the horizontal branch pipe 43, and is uniformly injected into the fluidized bed reactor at a certain speed and pressure through the nozzles 44.

[0098] (4) Mixing with the catalyst below and reaction: In the fluidized bed reactor, solid catalyst particles are lifted by the high-speed gas flow (mainly air) injected from above, forming a highly turbulent and boiling-like fluidized state. The mixture of methanol and ammonia injected from above immediately comes into full contact and rapid mixing with the highly dispersed and vigorously moving catalyst particles after entering the fluidized bed. This efficient gas-solid contact and mixing ensures that the reactant molecules can quickly adsorb onto the catalyst surface, thereby immediately initiating the exothermic catalytic oxidation reaction at high temperature to generate hydrocyanic acid. The reaction products (including hydrocyanic acid, by-products and unreacted raw materials) then exit from the top of the reactor and enter the subsequent separation and purification unit.

[0099] Example 2:

[0100] This embodiment provides a raw gas inlet distributor for a hydrocyanic acid fluidized bed reactor. As shown in Figure 1As shown, the raw material gas inlet distributor specifically comprises a low-stress inlet pipe 2 arranged on the reactor body 1, and a premixing chamber 3 and a raw material gas distributor 4 arranged in the reactor body 1.

[0101] Compared with example 1, as shown in the embodiment, the axial fins 34 are selected as corrugated plate fins. Figure 5 The single fin length of the corrugated plate fins is 2 m, and the thickness is 10 mm. The number of the corrugated plate fins in each horizontal premixing chamber 31 or vertical premixing chamber 32 is one or more.

[0102] Through the synergistic effect of the above technical improvements, the novel raw material gas inlet distributor can significantly improve the operation performance of the hydrocyanic acid fluidized bed reactor, and provide a more efficient, more stable and safer solution for the industrial production of hydrocyanic acid.

[0103] The above description of the embodiments is for facilitating the understanding and use of the utility model by ordinary skilled persons in the art. Those skilled in the art can easily make various modifications to the 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 according to the disclosure of the utility model without departing from the scope of the utility model should be within the protection scope of the utility model.

Claims

1. A feed gas inlet distributor for a hydrocyanic acid fluidized bed reactor, characterized in that, It includes a low-stress inlet pipe (2) installed on the reactor body (1), and a premixing chamber (3) and a raw material gas distributor (4) installed in the reactor body (1). The low-stress inlet pipe (2) is used to introduce high-temperature raw material gas. Specifically, it includes an inner pipe (21) that runs horizontally through the reactor body (1) and an outer pipe (22) that is arranged around the connection between the inner pipe (21) and the reactor body (1). A thermal expansion space (23) is formed between the outer pipe (22) and the outer wall of the inner pipe (21). The premixing chamber (3) includes at least one horizontal premixing chamber (31) connected to the inner pipe (21), and at least one vertical premixing chamber (32) connected to the horizontal premixing chamber (31); the horizontal premixing chamber (31) and the vertical premixing chamber (32) are provided with mixing auxiliary components along the axial direction for fully mixing the high-temperature raw material gas; The raw material gas distributor (4) includes an inlet main pipe (41), a horizontal branch pipe (42), a horizontal branch pipe (43), and a nozzle (44). The inlet main pipe (41) is connected to the vertical premixing chamber (32), the horizontal branch pipe (42) is connected to the inlet main pipe (41) and extends toward the inner wall of the reactor body (1), and the horizontal branch pipe (43) is connected to the horizontal branch pipe (42) and extends toward the inner wall of the reactor body (1). The nozzle (44) is set on the horizontal branch pipe (43) and is used to uniformly inject the preheated and premixed raw material gas into the reactor body (1).

2. The feed gas inlet distributor for a hydrocyanic acid fluidized bed reactor according to claim 1, characterized in that, The outer pipe (22) and the inner pipe (21) are connected by a flexible compensation connector (24); One end of the flexible compensation connector (24) is connected to the outer pipe (22), and the other end of the flexible compensation connector (24) is retracted to connect to the inner pipe (21).

3. The feed gas inlet distributor for a hydrocyanic acid fluidized bed reactor according to claim 2, characterized in that, The flexible compensation connector (24) includes an integrally connected straight section (241) and an arc-shaped connecting section (242). The straight section (241) is welded to the outer pipe (22), and the arc-shaped connecting section (242) is welded to the inner pipe (21).

4. The feed gas inlet distributor for a hydrocyanic acid fluidized bed reactor according to claim 1, characterized in that, The width of the thermal expansion space (23) is 20-40 mm.

5. The feed gas inlet distributor for a hydrocyanic acid fluidized bed reactor according to claim 1, characterized in that, The number of horizontal premixing chambers (31) is 3-5, and the number of vertical premixing chambers (32) is 5-10; The first horizontal premix chamber (31) is connected to the inner pipe (21) of the low-stress inlet pipe (2), and the remaining horizontal premix chambers (31) are connected in sequence. The first vertical premix chamber (32) is connected to the last horizontal premix chamber (31) through a through arc transition section (35); the remaining vertical premix chambers (32) are connected in sequence, and the last vertical premix chamber (32) is connected to the raw material gas distributor (4).

6. The feed gas inlet distributor for a hydrocyanic acid fluidized bed reactor according to claim 1, characterized in that, The length of a single section of the hybrid auxiliary component is 0.5-3m; A gap of 0.1-0.3m is left between the mixing auxiliary components in adjacent horizontal premixing chambers (31) or adjacent vertical premixing chambers (32).

7. The feed gas inlet distributor for a hydrocyanic acid fluidized bed reactor according to claim 1, characterized in that, The mixing auxiliary component is any one or a combination of two of the mixer (33) and axial fins (34); The mixer (33) is any one or more of the following: static baffle type, orifice plate type, and three-way type mixer; The axial fin (34) is any one or more of straight fins, spiral fins, or corrugated fins.

8. The feed gas inlet distributor for a hydrocyanic acid fluidized bed reactor according to claim 7, characterized in that, When the axial fins (34) are straight fins, the straight fins are evenly arranged circumferentially along the inner wall of the horizontal premixing chamber (31) or the vertical premixing chamber (32). The straight fins in adjacent horizontal premixing chambers (31) or vertical premixing chambers (32) are distributed at staggered angles.

9. The feed gas inlet distributor for a hydrocyanic acid fluidized bed reactor according to claim 1, characterized in that, The distribution area of ​​the nozzle (44) is divided into area A, area B and area C; Among them, the area located 25%-40% of the length of the horizontal branch pipe (43) is area A, the area located 20%-30% of the length of the horizontal branch pipe (43) is area B, and the area located 25%-35% of the length of the horizontal branch pipe (43) is area C.

10. A feed gas inlet distributor for a hydrocyanic acid fluidized bed reactor according to claim 9, characterized in that, The nozzle (44) in area A has an orifice diameter of 5-6.5 mm, while the nozzle (44) in areas B and C increases by 0.1-0.3 mm in each area.

Images