A production device and method for continuously synthesizing sodium amide

Abstract

The present application provides a method for continuously synthesizing sodium amide and a production device thereof. The method of the present application uses a primary reaction device, continuously adds sodium metal and ammonia gas, and makes the sodium metal react with the ammonia gas to generate sodium amide and hydrogen. The sodium metal and the sodium amide are stratified in the reaction device, the stratified sodium amide forms a settling zone at the lower part of the reaction device, and the sodium amide is continuously removed from the reaction device from the settling zone. The method has the advantages of process stability, low investment, few devices, high ammonia gas utilization rate, low energy consumption and convenient operation, overcomes the defects in the prior art that continuous production must use multiple reaction kettles, and especially overcomes the difficulty that a high-temperature pump must be used to remove the sodium amide product, and for the first time realizes single-tower continuous industrial production.

Description

Technical Field

[0001] The present invention relates to the technical field of sodium amide production, in particular to a production device and method for continuously synthesizing sodium amide. Background Art

[0002] Sodium amide is a compound with the molecular formula NaNH2 and a molecular weight of 39.0123. It is an olive green crystalline substance with a melting point of 210°C and a boiling point of 400°C. It decomposes into sodium hydroxide and ammonia in aqueous solution and decomposes into sodium, nitrogen, hydrogen, and ammonia when heated to 300-330°C in a vacuum. It decomposes violently in contact with water to produce sodium hydroxide and ammonia, but reacts more slowly in contact with ethanol. It is corrosive and hygroscopic.

[0003] Traditional sodium amide production typically involves melting solid sodium metal in an electric furnace, then heating it to around 300°C. Ammonia is then introduced to initiate the reaction. When the reactor temperature reaches 350±10°C, the furnace heating is stopped. As the amount of ammonia introduced increases, the exothermic reaction intensifies. Once the temperature reaches 380±10°C, a blower is used to cool the reactor until the reaction is complete. The blower is then used to lower the reactor temperature to 280±10°C, and the sodium amide is then transferred to the next process.

[0004] CN1944258A discloses a method for producing sodium amide, which comprises adding metallic sodium to a dry reactor replaced with ammonia, heating the reactor with an electric furnace under ammonia purge, introducing liquid ammonia when the reactor temperature rises to 200±20°C, stopping heating when the reactor temperature rises to 350-370°C, adjusting the flow of liquid ammonia to maintain the reactor temperature at 370-400°C until the reaction terminates, and slicing the sodium amide in the reactor after it cools to 250-300°C, using a drum slicer to obtain the finished product. The method employs a single-pot batch reaction, which not only has low production capacity and low ammonia utilization, but also is cumbersome to operate. Furthermore, during the ammonia reaction and the generation of hydrogen, an electric furnace is still used for heating for a period of time. When flammable and explosive hydrogen is generated, there is an open flame in the electric furnace, posing a major safety hazard.

[0005] CN101591009A discloses a method for continuously synthesizing sodium amide during indigo production. Liquid sodium metal is continuously added to a sodium amide pre-synthesis tower at a certain temperature. Liquid sodium metal is circulated through a sodium amide circulation pump. A portion of the liquid returns to the pre-synthesis tower to react with unreacted ammonia in the sodium amide synthesis tower at 300-400°C, with the tail gas discharged from the upper part of the tower. The remaining portion enters the sodium amide synthesis tower and reacts with ammonia at 300-400°C to produce sodium amide. The method uses a dual-tower circulation system, resulting in complex equipment and piping. Due to the high melting point of sodium amide, pipe blockage is very likely to occur during operation. The reaction process relies on a pump for circulation, which not only consumes a lot of power but also poses a difficult sealing problem at high temperatures. In the event of a leak, sodium amide is easily ignited when exposed to air, posing a significant safety risk. Furthermore, the tower is equipped with packing, which greatly complicates equipment maintenance.

[0006] CN102424407A discloses a device for continuously producing sodium amide. The device is a multi-stage fully mixed-flow reactor for continuously reacting metallic sodium with ammonia to produce sodium amide and hydrogen. The device utilizes a multi-reactor series reaction system to achieve a continuous production process. However, in addition to the problems faced by CN101591009A, it also faces the problems of higher investment, incomplete reaction (due to the fully mixed-flow reactor, the reaction endpoint is difficult to determine), and the sodium amide product contains a small amount of metallic sodium.

[0007] Therefore, it is urgent to provide an improved production device and method for continuously synthesizing sodium amide to solve the problems of the above-mentioned prior art. Summary of the Invention

[0008] The invention discloses a method for continuously synthesizing sodium amide. In a primary reaction device, metallic sodium and ammonia are continuously added, and the metallic sodium and the ammonia react to generate sodium amide and hydrogen. The metallic sodium and the sodium amide are separated into layers in the reaction device, and the metallic sodium layer is located above the sodium amide layer. The hydrogen and sodium amide are continuously removed from the reaction device, wherein the sodium amide is removed from a sedimentation zone formed by the accumulation of liquid sodium amide at the lower part of the reaction device.

[0009] According to the present invention, described sedimentation zone is a functional regional description rather than physical structural description.It is positioned at the bottom of reaction unit, and the liquid sodium amide generated by reaction converges and forms, and is sodium amide in the sedimentation zone, does not have or contains a small amount of sodium Metal 99.9, so in a sense, sedimentation zone also can be considered as the sodium amide layer, particularly after liquid sodium amide and liquid sodium Metal 99.9 layering, under the situation of no disturbance.The upper interface of sedimentation zone is the interface of sodium Metal 99.9 layer and sodium amide layer, and described interface is a zone with certain thickness in actual production, also referred to as the phase interface zone of sodium Metal 99.9 layer and sodium amide layer.

[0010] In the prior art sodium amide synthesis method, a sedimentation zone cannot be formed in a reaction device. The present invention controls the operation during the synthesis process so that liquid amino acid generated in the reaction device and liquid metallic sodium can be separated in layers, and the layered sodium amide can be gathered at the bottom of the reaction device to form a sedimentation zone. The sodium amide is removed from the sedimentation zone, thereby achieving the purpose of continuous feeding, continuous removal of sodium amide and hydrogen, and continuous synthesis of sodium amide.

[0011] Because the sedimentation zone is formed by the convergence of synthetic liquid sodium amide, the volume size of the sedimentation zone in the reaction unit is also dynamically changed in the whole continuous production process of the present invention. In the initial stage of the reaction, when sodium amide is not yet synthesized or the synthesis amount is less, the sedimentation zone does not exist or the volume is very small. Along with the synthesis increase of sodium amide in the reaction process, the sedimentation zone can progressively appear and the volume increases gradually, and the sedimentation zone upper interface can raise gradually. And, after stable production, if the shift-out rate of sodium amide is higher than the product synthesis rate, the sedimentation zone volume can reduce, and the upper interface of the sedimentation zone can reduce; if the shift-out rate of sodium amide is lower than the synthesis rate of sodium amide, the sedimentation zone volume can increase, and the upper interface of the sedimentation zone can raise.

[0012] To achieve the separation of liquid sodium amide and liquid metallic sodium into layers and form a sedimentation zone, it is necessary to provide conditions for the separation of the liquid sodium amide and liquid metallic sodium, and to minimize disturbance of the separated sodium amide so that it can settle to the bottom of the reaction apparatus to form a sedimentation zone. Furthermore, to maintain the high purity of the sodium amide in the sedimentation zone, disturbance of the sedimentation zone should also be minimized to maintain the high purity of the sodium amide removed from the discharge position in the sedimentation zone.

[0013] The present invention achieves the above-mentioned purpose by adjusting the height at which ammonia enters the reaction mass in the reaction unit as the reaction progresses, that is, the liquid sodium metal and liquid sodium amide in the reaction unit are separated into layers, and the sodium amide after separation can converge at the bottom of the reaction unit to form a sedimentation zone, and minimize the disturbance to the sedimentation zone. In the initial stage of the reaction, the material in the reaction unit is mainly sodium metal, and the height at which ammonia enters the reaction mass is located at a lower position in the reaction unit. As the reaction proceeds, sodium amide generation gradually increases, and the height at which ammonia enters the reaction mass is gradually increased accordingly. In some embodiments of the present invention, during the reaction process, the height at which ammonia enters the reaction mass is controlled in the sodium metal layer, and / or in the interface region between the sodium metal layer and the sodium amide layer, and / or in the upper part of the sedimentation zone, and the upper part of the sedimentation zone refers to the region between one-half of the sedimentation zone height and the upper interface of the sedimentation zone. By controlling the position at which ammonia enters the reaction mass in the above-mentioned region, the liquid sodium metal and liquid sodium amide in the reaction unit can be separated into layers, and the sodium amide after separation can form a sedimentation zone, and minimize the disturbance to the lower part of the sedimentation zone caused by the ammonia intake.

[0014] In some embodiments of the present invention, ammonia enters the reaction device through the air inlet pipe to react with metallic sodium. At this time, the position where the ammonia enters the reaction material in the reaction device is equivalent to the height of the air inlet pipe outlet. As the reaction proceeds, the height is controlled to be located in the metallic sodium layer and / or in the phase interface area and / or the upper part of the sedimentation area.

[0015] To increase the efficiency of the gas-liquid reaction, in a preferred embodiment of the present invention, the outlet of the inlet pipe is connected to a gas distributor, which distributes the ammonia gas into the sodium metal. When the gas distributor is connected, the height of the outlet of the inlet pipe is equivalent to the height of the gas distributor outlet.

[0016] According to the present invention, the gas distributor can be a conventional distributor in the art, including but not limited to distributors in shapes such as annular, calandria, coil, and conical. In some embodiments of the present invention, the gas distributor of the present invention is a perforated gas distributor, which can be a gas distributor with only one perforation or a gas distributor with two or more perforations.

[0017] In some embodiments of the present invention, in order to keep the gas outlet height of the gas distributor in the metallic sodium layer and / or in the phase interface zone and / or in the upper part of the sedimentation zone as the reaction proceeds, the gas outlet height of the gas distributor is adjustable.

[0018] In some embodiments of the present invention, the adjustable outlet height of the gas distributor in the reaction apparatus (equivalent to the height at which ammonia enters the feed) is achieved by a gas distributor with adjustable height. As the reaction proceeds, its height gradually rises from the bottom of the reaction apparatus to a position where the reaction stabilizes. In one embodiment of the present invention, the gas distributor is connected to an inlet pipe, and the portion of the inlet pipe within the reaction apparatus extends from the top to the bottom of the apparatus. The length of the portion of the inlet pipe within the reaction apparatus is adjustable.

[0019] In some embodiments of the present invention, the adjustable gas distributor outlet height in the reaction unit is by arranging a plurality of gas distributors at different height positions in the reaction unit, and the gas distributors at different height positions are enabled according to the reaction (corresponding to the height of the upper interface in the sedimentation zone) to realize. The gas distributors at these different height positions described, each can be a gas distributor with a fixed height, or each can be a gas distributor with a variable height within a certain range, or a combination of a gas distributor with a fixed height and a gas distributor with a variable height within a certain range, so as to realize the stepless change of the ammonia inlet position with the upper interface in the sedimentation zone. For example, 2, 3, 4 or 5 gas distributors at different heights can be set in the reaction unit, and during the reaction, the gas distributor at the height of the adaptation position is opened according to the upper interface in the sedimentation zone to realize the purpose of not causing disturbance below the sedimentation zone as much as possible. In one embodiment of the present invention, 2 or 3 gas distributors at different height positions are set in the reaction unit, and the height of these gas distributors is fixed.

[0020] According to the present invention, in the synthesis method, the ratio of raw materials added is: metallic sodium: ammonia (mass ratio) = 1: 0.74-1.08.

[0021] According to the present invention, in the synthesis method, the reaction temperature is controlled within the range of 300-400°C.

[0022] According to the present invention, the sodium metal added to the reaction device is solid sodium metal or liquid sodium metal, preferably liquid sodium metal at a temperature of 100°C to 300°C, and in particular liquid sodium metal at a temperature below 200°C. Liquid sodium metal is more convenient for continuous input into the reaction device, and after entering the reaction device, the low-temperature liquid sodium metal can be heated to a higher temperature conducive to the synthesis reaction by the reaction heat generated in the reaction device, thereby facilitating the comprehensive utilization of reaction heat and reducing energy consumption.

[0023] When solid sodium metal is used as the raw material, it can be added to the reaction apparatus using conventional solid addition devices or methods, such as screw conveyor. At the initial stage of the reaction, the solid sodium metal added to the reaction apparatus can be converted into liquid sodium metal by external heating. Once the reaction stabilizes and generates reaction heat, subsequent additions of solid sodium metal can be converted into liquid sodium metal by the released reaction heat.

[0024] In another embodiment of the present invention, solid sodium metal can be preheated using the heat of reaction to form liquid sodium metal before being introduced into the reaction apparatus. In a specific embodiment of the present invention, a jacket is provided outside the reaction apparatus, solid sodium metal is introduced into the jacket, preheated and melted using the heat of reaction to form liquid sodium metal, and then introduced into the reaction apparatus.

[0025] If necessary, a heating device can be provided on the outer surface of the reaction device. The heating device can be heated by conventional methods in the art, such as electric heating, steam, thermal oil, or molten salt. In one embodiment of the present invention, an electric heater is used, which is installed on the outer wall of the reaction device (such as a synthesis reaction tower).

[0026] If necessary, a cooling device can be provided outside the reaction device. The cooling device can adopt conventional methods in the art, such as a fan, a cooling jacket, etc., so as to perform cooling treatment when the reaction temperature exceeds 400°C.

[0027] Sodium amide is removed from the reaction device from a discharge position located in the sedimentation zone. In one embodiment of the present invention, the discharge position is a discharge port opened at the bottom of the reaction device body (i.e., the bottom of the sedimentation zone), and the discharge port is connected to a sodium amide storage device outside the reaction device through a pipeline.

[0028] In another embodiment of the present invention, the discharge position is located at the lower part of the sedimentation zone inside the reaction device, and the discharge pipe is inserted into the sedimentation zone, so that the opening position of the discharge pipe is located at the discharge position, and the material pressure in the reaction device is used to press sodium amide into the discharge pipe and into the sodium amide storage device connected thereto; or, sodium amide is sent into the sodium amide storage device connected thereto through the discharge pipe by external suction.

[0029] Sodium metal reacts with ammonia to form hydrogen. This hydrogen and any unreacted ammonia form tail gas, which is then discharged from the reactor. This tail gas can subsequently be treated. The tail gas can be discharged from the reactor through a gas outlet located at the top of the reactor. This gas outlet can be connected to a tail gas recovery device.

[0030] According to the present invention, the tail gas treatment includes separating ammonia and hydrogen, and the separated ammonia and hydrogen are respectively purified to recover the ammonia and hydrogen. The hydrogen is used as fuel or for other industrial purposes. The separated ammonia can be recycled and reused in the synthesis method of the present invention.

[0031] In one embodiment of the present invention, the tail gas treatment method is to remove ammonia in the tail gas by water washing to form ammonia water and hydrogen; the ammonia water is distilled to obtain recovered ammonia, and the hydrogen is further refined and recovered by water washing, acid washing, alkali washing and other methods.

[0032] In one embodiment of the present invention, a method for continuously synthesizing sodium amide is disclosed. The method uses a primary synthesis reaction tower, the reaction tower is provided with a feed port, an air inlet pipe, a gas discharge port, and a gas distributor connected to the air inlet pipe and having an adjustable height is provided in the reaction tower so that the height at which ammonia enters the material can be adjusted. The method comprises: continuously adding metallic sodium into the synthesis reaction tower, continuously introducing ammonia through the gas distributor, the synthesized sodium amide and metallic sodium are separated into layers and converge at the lower part of the reaction tower to form a sedimentation zone, during the reaction, the position of the gas distributor is adjusted so that its height is higher than or equal to the upper half of the height of the sedimentation zone, sodium amide is removed from the discharge position at the lower part of the sedimentation zone, and hydrogen generated by the reaction and any unreacted ammonia are discharged through the gas discharge port of the reaction tower.

[0033] The height-adjustable gas distributor can be a single height-adjustable gas distributor or a plurality of gas distributors at different heights. The height of each of these gas distributors at different heights is fixed. The gas distributor at the corresponding position is activated according to the height of the upper interface of the sedimentation zone to achieve the purpose of preventing the ammonia gas from disturbing the sedimentation zone as much as possible. For example, 2, 3, 4 or 5 gas distributors at different heights can be set, and preferably 2 or 3 gas distributors at different heights are set.

[0034] The method for continuously synthesizing sodium amide of the present invention can be divided into two stages during actual operation: a startup stage and a stable reaction stage.

[0035] During the startup phase, metallic sodium is added to the reaction device, and the heating device is turned on to raise the temperature to 300-400°C. Ammonia is allowed to enter the reaction mass from the lower part of the reaction device. As the sodium amide liquid level in the reaction device (equivalent to the upper interface of the sedimentation zone) gradually rises, the height at which ammonia enters the reaction mass in the reaction device is adjusted accordingly. When the sodium amide liquid level reaches a preset height position, the startup phase is completed and the stable reaction phase is entered. In actual production, a density meter can be installed at a preset height position in the reaction device to detect the density of the material at the density meter. When the density reaches 1.3g / cm 3 After that, the startup phase can be considered completed and the stable reaction phase can be entered. In actual production, this can also be determined by monitoring the exhaust gas composition. When the ammonia content in the exhaust gas begins to be less than 25%, the startup phase can be considered completed and the stable reaction phase can be entered.

[0036] During the stable reaction phase, the reaction heat is utilized to maintain the reaction, and the heating device can be shut down or operated at a reduced load. By adjusting the amounts of sodium metal and ammonia added and, if necessary, cooling the reaction temperature, the reaction temperature is controlled within the range of 300-400°C. The sodium amide liquid level is maintained relatively stable, and the height at which ammonia enters the reaction apparatus is also relatively stable, above the upper half of the height of the sodium amide settling zone. This minimizes disturbance of the settling zone and facilitates removal of the sodium amide product from the discharge point located in the settling zone. During the stable reaction phase, the weight ratio of sodium metal to ammonia can be 1:0.74-1.08. Due to the improved synthesis process of the present invention, the ammonia conversion rate is significantly improved. During the stable reaction phase, the weight ratio of sodium metal to ammonia can also be controlled within a smaller range, for example, 1:0.74-0.82.

[0037] In one embodiment of the present invention, three gas distributors are arranged in ascending order of height within a synthesis reaction tower. During the startup phase, metallic sodium is added to the synthesis reaction tower through a feed port, and the heating device is activated to raise the temperature to 300-400°C. Ammonia gas is introduced by opening the lowest gas distributor within the reaction unit until the sodium amide liquid level within the reaction unit exceeds a preset height, completing the startup phase and entering the stable reaction phase.

[0038] During the stable reaction phase, the reaction heat is used to maintain the reaction. The lowest gas distributor in the reactor is closed, and the gas distributors at intermediate and / or higher heights are opened. A settling zone is formed between the bottom of the tower and the gas distributor at the middle height. The sodium amide product is removed from the discharge port located in the settling zone. During the stable reaction phase, metallic sodium and ammonia are continuously added, and the reaction temperature is controlled within the range of 300-400°C. Hydrogen and ammonia are removed from the upper portion of the reactor, and the sodium amide product is removed from the settling zone.

[0039] The present invention also discloses a device for continuously synthesizing sodium amide, comprising a reaction device, wherein the reaction device is provided with a feeding port, an air inlet component, and a gas discharge port. The device is characterized in that the lower part of the reaction device is a sedimentation zone, the discharge position of sodium amide is arranged at the lower part of the sedimentation zone, and the gas outlet height position of the air inlet component in the reaction device is adjustable.

[0040] According to the present invention, the air intake assembly includes an air intake pipe and a gas distributor connected to the air intake pipe.

[0041] In one embodiment of the present invention, the air intake assembly includes an air intake pipe and a gas distributor connected to the air intake pipe. The portion of the air intake pipe within the reaction device extends from the upper part of the device to the lower part of the device, and the length of the portion of the air intake pipe within the reaction device is telescopically adjustable.

[0042] In one embodiment of the present invention, the air intake assembly includes an air intake pipe and at least two gas distributors connected to the air intake pipe. The portion of the air intake pipe within the reactor extends from the upper portion of the reactor to the lower portion of the reactor. Each of the gas distributors is connected to the portion of the air intake pipe within the reactor and is positioned at a different height on the air intake pipe. For example, the air intake assembly includes an air intake pipe and three gas distributors connected to the air intake pipe, each of the three gas distributors being positioned at a different height on the air intake pipe.

[0043] In one embodiment of the present invention, the air intake assembly includes at least two air intake pipes and a gas distributor connected to each air intake pipe. The portion of each air intake pipe within the reaction apparatus extends from the upper portion to the lower portion of the apparatus, and each gas distributor is positioned at a different height within the reaction apparatus. For example, the air intake assembly includes three air intake pipes and a gas distributor connected to each air intake pipe. The three gas distributors are positioned at different heights within the reaction apparatus and may be referred to, from bottom to top, as a first gas distributor, a second gas distributor, and a third gas distributor.

[0044] According to the present invention, a charging port is used to add sodium metal to the reaction apparatus. The charging port can be located at the top, upper portion, or center of the reaction apparatus. To reduce disturbance to the settling zone within the reaction apparatus, the charging port is preferably connected to a delivery conduit within the reaction apparatus, through which the sodium metal is transported within the reaction apparatus. In one embodiment of the present invention, the charging port is located at the top of the reaction apparatus, and a delivery conduit extends from the charging port to the center of the reaction apparatus.

[0045] Furthermore, the device further comprises a heating device disposed outside the reaction device. In one embodiment of the present invention, the heating device is an electric heater.

[0046] Furthermore, a jacket layer is provided outside the reaction apparatus, and the jacket layer is used to store the solid sodium metal to be preheated. In one embodiment of the present invention, the apparatus further includes a liquid sodium metal storage device, which is connected to the jacket layer to store the liquid sodium metal formed by preheating. In one embodiment of the present invention, the apparatus further includes a pump, which is connected to the jacket layer, the liquid sodium metal storage device, and the feed port of the reaction apparatus to pump the liquid sodium metal between the jacket layer, the liquid sodium metal storage device, and the reaction apparatus.

[0047] Furthermore, the device further comprises a cooling device disposed outside the reaction device. In one embodiment of the present invention, the cooling device is a fan.

[0048] Furthermore, the apparatus further comprises a sodium amide storage device disposed outside the reaction unit. The sodium amide storage device is connected to a sodium amide removal pipeline in the reaction unit. In one embodiment of the present invention, a discharge port is disposed at the bottom of the reaction unit body, and the sodium amide removal pipeline is connected to the discharge port. In one embodiment of the present invention, the sodium amide removal pipeline is inserted into a discharge position located in the settling zone.

[0049] Furthermore, the device also includes an exhaust gas treatment device connected to the gas exhaust port of the reaction device. In one embodiment of the present invention, the exhaust gas treatment device includes a device for separating ammonia and hydrogen. The exhaust gas treatment device also includes a device for separating and recovering ammonia and a device for purifying hydrogen.

[0050] In one embodiment of the present invention, a production apparatus for the continuous synthesis of sodium amide is provided, comprising a synthesis reaction tower, the synthesis reaction tower being provided with a feeding pipe for feeding sodium metal, a gas distributor being provided within the synthesis reaction tower, the gas distributor being connected to an inlet pipe for introducing ammonia gas, a heating device being provided within the synthesis reaction tower, a sodium amide storage tank being connected to the bottom of the synthesis reaction tower, and a gas discharge pipe being provided at the top of the synthesis reaction tower. Preferably, the heating device is an electric heater mounted on the outer wall of the synthesis reaction tower. Preferably, the sodium metal is liquid sodium metal at a temperature of 120±10°C. Preferably, the feeding pipe is mounted at the top of the synthesis reaction tower and is provided with a flow meter. Preferably, the gas distributor is a vent coil, each vent coil being connected to an inlet pipe, and the inlet pipe being mounted at the top of the synthesis reaction tower. Preferably, there are three ventilation coils from bottom to top, and the three ventilation coils from bottom to top are respectively connected to the first air inlet pipe, the second air inlet pipe and the third air inlet pipe. Preferably, the gas exhaust pipe is connected to an exhaust gas recovery device.

[0051] In one embodiment of the present invention, a production method based on the above-mentioned continuous synthesis of sodium amide production device is provided, including a reaction started by a heating device and a reaction maintained by reaction heat; the reaction started by the heating device comprises: continuously adding metallic sodium into the synthesis reaction tower through the feeding pipe, pausing the feeding after the feeding is completed, then turning on the heating device to heat up to a specified temperature, and then turning off the heating device; then opening the gas distributors from bottom to top in sequence to introduce ammonia, and adding metallic sodium during the intervals when the gas distributors are opened; then closing the gas distributor at the bottom, and opening the bottom of the synthesis reaction tower from the bottom to the top. The sodium amide product is continuously discharged into the sodium amide storage tank at the beginning, and the liquid level is kept relatively stable, and the material is continuously fed and discharged. The hydrogen generated by the reaction and the unreacted ammonia are discharged into the tail gas recovery device through the gas discharge pipe; the reaction maintained by using the reaction heat includes: after the reaction is started, metallic sodium is continuously added into the synthesis reaction tower, and then the gas distributor is opened to control the reaction temperature. The synthesized sodium amide is continuously discharged from the bottom of the synthesis reaction tower into the sodium amide storage tank, and the liquid level is kept relatively stable to achieve continuous feeding and discharging. The hydrogen generated by the reaction and the unreacted ammonia are discharged into the tail gas recovery device through the gas discharge pipe.

[0052] In the present invention:

[0053] "Reaction material" and "material" have the same meaning: it refers to the material in the reaction process, which includes the raw material sodium metal, a mixture of sodium metal and sodium amide, and / or the product sodium amide.

[0054] The lower part of the reaction device generally refers to the lower part of the reaction device, usually relative to the upper part. In the present invention, the lower part is often the reaction area and product settling area.

[0055] The settling zone is a functional area in the reaction unit, and this area is used to sediment high-density products. The present invention cleverly utilizes the characteristic that the density of liquid sodium amide is greater than that of liquid metallic sodium, sets the settling zone at the bottom of the reaction unit, and controls the height of ammonia gas entering the material to be adjustable, so that sodium amide and metallic sodium can be separated and converged in the settling zone after layering in the reaction unit, and avoids the agitation of ammonia gas and makes the sodium amide in the settling zone relatively static. It will be appreciated by those skilled in the art that in the present invention, the settling zone is usually located in the area between the bottom of the reaction unit and the ammonia gas distributor in the open state. Of course, the division of the settling zone is not very strict. In many cases, the gas distributor may be located at a position more than half of the upper height of the preset settling zone, as long as it is ensured that the sodium amide located at the discharge position of the settling zone does not contain or hardly contains metallic sodium. In other words, the settling zone is located below the gas distributor of the air intake, which is convenient for the sodium amide sedimentation layering.

[0056] Beneficial technical effects:

[0057] 1. The inventors of the present invention unexpectedly discovered and cleverly utilized the principle of the density difference between metallic sodium and sodium amide. By controlling the height at which ammonia gas enters the material, a sedimentation zone is formed inside the device during the reaction process, so that the synthesized sodium amide can settle to the lower part of the reaction tower, while the unreacted metallic sodium is concentrated in the middle and upper part of the reaction tower due to its low density. This overcomes the defects of the prior art that continuous production must use multiple reactors, especially the difficulty of using a high-temperature pump to remove the sodium amide product, and realizes single-tower continuous industrial production for the first time.

[0058] 2. The present invention adopts a single-tower continuous reaction, avoiding the use of a high-temperature pump to remove the product, thus solving the maintenance and leakage problems caused by the instability of the high-temperature pump in multi-tower continuous reactions. In particular, the safety and environmental pollution problems of handling dangerous sodium amide during shutdown (normal or abnormal) are solved.

[0059] 3. The process of the present invention has the advantages of stable process, low investment, few equipment, high ammonia utilization rate (the original intermittent reaction requires a 45%-50% excess of ammonia, while the method of the present invention only requires a 5%-10% excess of ammonia, and the ammonia utilization rate is increased by more than 35% compared with the original), low energy consumption, and easy operation. It is convenient for large-scale centralized production of sodium amide, and has significant economic, environmental and safety benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0060] Figure 1 This is a schematic diagram of an arrangement of a production device for continuous synthesis of sodium amide according to the present invention;

[0061] Figure 2 This is a schematic diagram of another arrangement of the production device for continuous synthesis of sodium amide of the present invention;

[0062] Figure 1 and Figure 2 Middle: 1-synthesis reaction tower, 2-electric heater, 3-sodium amide storage tank, 4-third gas distributor, 4'-second gas distributor, 4"-first gas distributor, 5-feeding pipe, 6-gas discharge pipe, 7-first air inlet pipe, 8-second air inlet pipe, 9-third air inlet pipe, 10-sedimentation zone, 11-discharge position

[0063] Figure 3 It is an embodiment of a height-variable gas distributor, wherein 4-gas distributor, 9-air inlet pipe, 12-height adjustment mechanism

[0064] Figure 4 This is a schematic diagram of the functional areas inside the reaction device during the reaction, 13-gas phase space, 14-metal sodium layer, 15-phase interface area, 16-sodium amide layer

[0065] Figure 5 This is a schematic diagram of a reaction device with a jacket layer for preheating solid sodium metal of the present invention, 1-synthesis reaction tower, 2-electric heater, 4-gas distributor, 6-gas discharge pipe, 9-air inlet pipe, 11-discharge position, 12-height adjustment mechanism, 17-jacket layer, 18-liquid sodium metal storage tank, 19-pump, 20-sodium amide discharge pipe DETAILED DESCRIPTION

[0066] The following will clearly and completely describe the technical solutions in the embodiments of the present invention in conjunction with the accompanying drawings. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative efforts are within the scope of protection of the present invention.

[0067] Example 1

[0068] like Figure 2 As shown, this embodiment provides an embodiment of the production device for continuous synthesis of sodium amide of the present invention, comprising a synthesis reaction tower 1, an electric heater 2 installed at the lower part of the outside of the synthesis reaction tower 1, and a sodium amide storage tank 3 located outside the synthesis reaction tower 1. A first gas distributor 4", a second gas distributor 4' and a third gas distributor 4 are arranged from low to high inside the synthesis reaction tower 1, and are respectively connected to a first air inlet pipe 7, a second air inlet pipe 8 and a third air inlet pipe 9. The portion of each air inlet pipe inside the reaction device extends from the upper part of the device to the lower part of the device. A feeding pipe 5 and a gas discharge pipe 6 are also provided at the top of the synthesis reaction tower. Below the interior of the synthesis reaction tower 1 is a sedimentation zone 10. A discharge position 11 is located in the sedimentation zone 10, and a pipeline is drawn out from the discharge position 11 to connect to the sodium amide storage tank 3.

[0069] The process flow for producing sodium amide using the device of this embodiment is as follows: liquid metallic sodium is continuously added to the synthesis reaction tower 1 through the feeding pipe 5, the electric heater 2 is turned on to raise the temperature in the synthesis reaction tower to 350±10°C, and then the electric heater 2 is turned off. Then, according to the progress of the reaction, the first gas distributor 4", the second gas distributor 4' and the third gas distributor 4 corresponding to the first air inlet pipe 7, the second air inlet pipe 8 and the third air inlet pipe 9 are opened in sequence to introduce ammonia gas, so that the ammonia inlet height can be adjusted according to the height of the sodium amide liquid level, and the disturbance of the sedimentation zone by the ammonia inlet is avoided as much as possible. The hydrogen produced by the reaction and the unreacted ammonia are discharged from the synthesis reaction tower 1 through the gas discharge pipe 6 and can be discharged into the tail gas recovery device. The synthesized sodium amide is removed from the discharge position 11 set in the bottom sedimentation zone 10 of the synthesis reaction tower 1 and sent to the sodium amide storage tank 3.

[0070] Those skilled in the art will understand that Figure 1Also provided is a production device for continuously synthesizing sodium amide within the scope of the present invention, which is Figure 2 The only difference is the way in which sodium amide is removed from the synthesis reaction tower 1. Figure 1 A discharge port is opened at the bottom of the reaction device body, and the discharge port is connected to the sodium amide storage tank 3 through a pipeline, and the sodium amide is sent into the storage tank through the discharge port.

[0071] According to the concept of the present invention, those skilled in the art can make various modifications to the reaction device (such as adjusting the position of the air inlet pipe entering the synthesis reaction tower, adjusting the position of the feeding pipe entering the reaction synthesis tower, adjusting the position of the gas exhaust pipe exiting the reaction synthesis tower, adjusting the path for sodium amide to be removed from the reaction synthesis tower, etc.), which all fall within the protection scope of the present invention.

[0072] Example 2

[0073] like Figure 3 As shown, this embodiment provides an example of a height-adjustable air intake assembly, which is composed of an air intake pipe 9 and a gas distributor 4, wherein the length of the air intake pipe is adjusted by a height adjustment mechanism 12. The height-adjustable air intake assembly in this embodiment can replace Figure 1 and Figure 2 The first air inlet pipe 7, the second air inlet pipe 8, the third air inlet pipe 9 and the first gas distributor 4", the second gas distributor 4' and the third gas distributor 4 connected thereto are installed in the synthesis reaction tower 1, so that the height of the gas distributor 4 can be adjusted up and down, thereby achieving the adjustable height of the ammonia gas inlet to minimize the disturbance of the settling zone by the ammonia gas inlet.

[0074] Those skilled in the art can Figure 3 Within the conceptual framework of the height-adjustable air intake assembly shown, various modifications are made (for example, changing the connection point between the air intake pipe 9 and the gas distributor 4, changing the shape of the gas distributor 4, changing the height adjustment structure 12 to a telescopic tube, etc.), and the various modifications do not deviate from Figure 3 The improvements to the core points of the height-adjustable air intake assembly shown are all within the scope of protection of the present invention.

[0075] Example 3

[0076] Figure 4 This image shows the separation of the raw sodium metal and the product sodium amide into layers within the reactor during the reaction process, with the sodium metal layer at the top and the sodium amide layer at the bottom. Above the sodium metal layer is the gas phase, and between the sodium metal and sodium amide layers is the transitional interface.

[0077] Figure 4 The stratification of the reaction materials in the reaction device during the reaction process under ideal conditions is shown. Figure 1 、 Figure 2 The structure of the reaction synthesis tower and its internal air inlet pipe and gas distributor, and Figure 3 The purpose of the inlet assembly is to ensure that the stratification of the reactants in the reactor during actual production is as close to this ideal state as possible. In particular, by adjusting the ammonia inlet height, the disturbance of the sodium amide layer by the ammonia inlet during the reaction is minimized, creating a settling zone that provides a pure sodium amide discharge environment. However, in actual production, the interphase zone can undergo significant fluctuations due to the bubbling and agitation of the ammonia inlet.

[0078] Example 4

[0079] like Figure 5 As shown, another embodiment of the continuous synthesis of sodium amide production device of the present invention is provided in this embodiment. A jacket layer 17 is provided outside the synthesis reaction tower 1, and an electric heater 2 is provided outside the jacket layer 17. There is also a liquid metal sodium storage tank 18 and a pump 19 connected by pipelines. The liquid metal sodium is transported between the jacket layer 17, the liquid metal sodium storage tank 18 and the synthesis reaction tower feed port by the pump 19. The discharge position 11 is located in the sedimentation zone, and the sodium amide discharge pipe 20 extends from this position to the top of the synthesis reaction tower 1 to discharge the product sodium amide from the synthesis reaction tower 1. The height adjustment mechanism 12 on the air inlet pipe 9 makes the height of the gas distributor 4 in the reaction device adjustable.

[0080] At the start of the reaction, solid metallic sodium is added to the jacket layer 17, heated and liquefied, and then returned to the liquid metallic sodium storage tank 18. The low-temperature metallic sodium in the liquid metallic sodium storage tank 18 is then heated and circulated through the sodium pump 19 and sent to the jacket layer 17, or sent to the synthesis reaction tower 1 according to the reaction requirements.

[0081] Those skilled in the art can modify the reaction device according to the concept of the present invention, for example, the air inlet pipe 9, the height adjustment mechanism 12 and the gas distributor 4 connected thereto can be used as follows: Figure 1 and 2 The first air inlet pipe 7, the second air inlet pipe 8, the third air inlet pipe 9 and the corresponding first gas distributor 4", the second gas distributor 4' and the third gas distributor 4 are replaced, or Figure 5 On the basis of Figure 1 and 2 The first air inlet pipe 7, the second air inlet pipe 8 and the corresponding first gas distributor 4", the second gas distributor 4', etc. are changed, and the placement position and related arrangements of the electric heater 2, the jacket layer 17, and the sodium amide discharge pipe 20 are changed.

[0082] Example 6: Implementation method in the startup phase

[0083] use Figure 2 reaction device.

[0084] Liquid metallic sodium (125-135°C) is continuously added to the synthesis reaction tower 1 through the feeding pipe 5 at a rate of 1000kg / h. After 3 hours of feeding, the feeding is suspended, and then the electric heater 2 is turned on to raise the temperature to 345°C, and then the electric heater 2 is turned off. The first air inlet pipe 7 is opened to introduce ammonia through the first gas distributor 4" at a rate of 800kg / h. The reaction is carried out for 2 hours, and then the feeding pipe 5 for metallic sodium is opened again. After continuing to feed for 2 hours, the second air inlet pipe 8 is opened to introduce ammonia through the second gas distributor 4'. After continuing to feed for 4 hours, the third air inlet pipe 9 is opened to introduce ammonia through the third gas distributor 4, and then the first gas distributor 4" is closed. The ammonia rate is maintained at 800kg / h during the entire process. The tail gas released from the gas discharge pipe 6 is detected. When the ammonia content in the tail gas reaches about 25%, the liquid level of sodium amide has basically reached the gas outlet height of the first gas distributor 4". At this time, it can be considered that the startup phase is completed, and then the stable continuous production phase is entered.

[0085] Example 7

[0086] After entering the stable stage from the start-up stage of Example 6, liquid metallic sodium (125-135° C.) was continuously added at a rate of 1000 kg / h. During this stage, the first air inlet pipe 7 and the first gas distributor 4″ connected thereto were closed, the second air inlet pipe 8 and the third air inlet pipe 9 were opened, and ammonia was introduced through the second and third gas distributors 4′ and 4, respectively. The total flow rate of ammonia added was 780 kg / h, and the reaction temperature was 348.1° C. During the stable reaction, the inlet rate of metallic sodium and / or ammonia was adjusted. The reaction temperature is controlled within the range of 345-360°C by adjusting the feed rate. For example, when the reaction temperature approaches the upper limit, the feed rate is reduced; when the reaction temperature approaches the lower limit, the feed rate is increased. Sodium amide product is continuously removed from the discharge port of the settling zone of the synthesis reaction tower 1 to the sodium amide storage tank 3. The sodium amide removal rate is based on maintaining a relatively stable sodium amide liquid level in the reaction tower. The reaction tail gas, including generated hydrogen and unreacted ammonia (9.96% in the tail gas), is discharged into the tail gas recovery device through the gas discharge pipe 6.

[0087] Compared with the original intermittent production, this method can save about 400 degrees of electricity and about 220 kg of ammonia for each ton of metallic sodium heated to the reaction temperature through electric heating, and can shorten the heating time by about 4 hours.

[0088] Example 8

[0089] After entering the stable phase from the start-up phase of Example 6, liquid sodium metal (125-135 ℃) was continuously added, and the addition amount was continuously added at 1500kg / h. In this stage, the first air inlet pipe 7 and the first gas distributor 4 "connected thereto were closed, the second air inlet pipe 8 and the third air inlet pipe 9 were opened, and ammonia was fed via the second and third gas distributors 4 ' and 4, respectively. The total flow rate of ammonia added was 1180kg / h, and the reaction temperature was 354.8 ℃. In the stable phase, the amount of sodium metal 9 and / or ammonia introduced was regulated to control the reaction temperature within the range of 345-360 ℃. The sodium amide product was continuously shifted out from the discharge port in the settling zone of the synthesis reaction tower 1 to the sodium amide storage tank 3, and the shift-out rate of sodium amide was based on the relative stability of the sodium amide liquid level in the reaction tower. The reaction tail gas, comprising the hydrogen produced and unreacted ammonia (content 11.4% in the tail gas), was discharged into the tail gas recovery device through the gas discharge pipe 6.

[0090] Compared with the original intermittent production, this method can save about 600 degrees of electricity and about 330 kg of ammonia for heating each ton of metallic sodium to the reaction temperature through electric heating, and can shorten the heating time by about 4.5 hours.

[0091] Example 9

[0092] After entering the stable phase from the startup phase of Example 6, liquid sodium metal (125-135 ℃) is continuously added, and the addition amount is continuously added at 1000kg / h. In this stage, the first air inlet pipe 7 and the third air inlet pipe 9 and the first and third gas distributors 4 " and 4 connected thereto are closed, and the second air inlet pipe 8 and the second gas distributor 4' connected thereto are kept open to feed ammonia. The total flow rate of ammonia added is 790kg / h, and the reaction temperature is 347.5 ℃. The amount of sodium metal and / or ammonia introduced is adjusted to control the reaction temperature within the range of 345-360 ℃. The sodium amide product is continuously removed from the discharge port in the settling zone of the synthesis reaction tower 1 to the sodium amide storage tank 3, and the removal rate of sodium amide is based on keeping the sodium amide liquid level in the reaction tower relatively stable. The reaction tail gas comprises the hydrogen produced and unreacted ammonia (content 12.10% in the tail gas), which is discharged into the tail gas recovery device through the gas discharge pipe 6.

[0093] Compared with the original intermittent production, this method can save about 400 degrees of electricity and about 220 kg of ammonia for each ton of metallic sodium heated to the reaction temperature through electric heating, and can shorten the heating time by about 4 hours.

[0094] Example 10

[0095] After entering the stable phase from the start-up phase of Example 6, liquid sodium metal (125-135° C.) was continuously added, and the addition rate was continuously increased at 1500 kg / h. In this phase, the first air inlet pipe 7 and the third air inlet pipe 9 and the first and third gas distributors 4 ″ and 4 ″ connected thereto were closed, and the second air inlet pipe 8 and the second gas distributor 4 ′ connected thereto were kept open to feed ammonia. The total flow rate of ammonia added was 1210 kg / h, and the reaction temperature was 353.2° C. In the stable phase, the amount of sodium metal metal and / or ammonia introduced was adjusted to control the reaction temperature within the range of 345-360° C. The sodium amide product was continuously removed from the discharge port in the settling zone of the synthesis reaction tower 1 to the sodium amide storage tank 3, and the removal rate of sodium amide was such as to keep the sodium amide liquid level in the reaction tower relatively stable. The reaction tail gas, comprising the generated hydrogen and unreacted ammonia (content 15.45% in the tail gas), was discharged into the tail gas recovery device through the gas discharge pipe 6.

[0096] Compared with the original intermittent production, this method can save about 600 degrees of electricity and about 330 kg of ammonia for heating each ton of metallic sodium to the reaction temperature through electric heating, and can shorten the heating time by about 4.5 hours.

[0097] The present invention uses specific examples to illustrate the principles and implementation methods of the present invention. The above examples are only intended to help understand the method and core concept of the present invention. At the same time, those skilled in the art will find that the specific implementation methods and application scopes may vary based on the concept of the present invention. In summary, the contents of this specification should not be understood as limiting the present invention.

Claims

1. A method for continuously synthesizing sodium amide, characterized in that, In a primary reaction device, sodium metal and ammonia are continuously added, and the sodium metal reacts with the ammonia to generate sodium amide and hydrogen. The sodium metal and sodium amide are separated into layers in the reaction device, and the sodium metal layer is located above the sodium amide layer. Hydrogen and sodium amide are continuously removed from the reaction device, wherein the sodium amide is removed from a sedimentation zone formed by the convergence of liquid sodium amide at the lower part of the reaction device. The air inlet height of the ammonia in the reaction device is adjustable. As the reaction proceeds, the position where the ammonia enters the reaction materials in the reaction device is controlled to be located in the sodium metal layer, and / or in the interface zone between the sodium metal layer and the sodium amide layer, and / or in the upper part of the sedimentation zone. The upper part of the sedimentation zone refers to the area between one-half of the height of the sedimentation zone and the upper interface of the sedimentation zone.

2. The method according to claim 1, wherein Ammonia enters the reaction device through an air inlet pipe to react with metallic sodium. The outlet of the air inlet pipe is connected to a gas distributor, and the ammonia is distributed into the metallic sodium through the gas distributor. The gas outlet height position of the gas distributor in the reaction device is adjustable. As the reaction proceeds, the position of the gas distributor is controlled to be in the metallic sodium layer, and / or in the interface area between the metallic sodium layer and the sodium amide layer, and / or in the upper part of the sedimentation zone.

3. The method according to claim 2, wherein A gas distributor with adjustable height is used to achieve the adjustable gas outlet height of the gas distributor; or, multiple gas distributors at different heights are set in the reaction device, and gas distributors at different positions are activated according to the reaction progress to achieve the adjustable gas outlet height of the gas distributor.

4. The method according to claim 3, wherein The height-adjustable gas distributor is connected to the air inlet pipe. The portion of the air inlet pipe inside the reaction device extends from the upper part of the device to the lower part of the device. The length of the portion of the air inlet pipe inside the reaction device is telescopically adjustable.

5. The method according to claim 3, wherein Each of the multiple gas distributors at different heights is a gas distributor with a fixed height; or each is a gas distributor with a height that is variable within a certain range; or is a combination of a gas distributor with a fixed height and a gas distributor with a height that is variable within a certain range.

6. The method according to claim 2, wherein 2, 3, 4 or 5 gas distributors at different heights are set in the reaction device. During the reaction process, the gas distributor with the appropriate height is opened according to the upper interface of the sedimentation zone.

7. The method according to any one of claims 1 to 6, wherein: The ratio of raw materials added is: mass ratio of metallic sodium to ammonia gas = 1: 0.74-1.08; the reaction temperature is controlled within the range of 300-400°C.

8. The method according to any one of claims 1 to 6, wherein: The sodium metal is added to the reaction device in the form of liquid sodium metal, a jacket layer is provided outside the reaction device, solid sodium metal is added to the jacket layer, preheated and melted by reaction heat to form liquid sodium metal, and then the liquid sodium metal is fed into the reaction device; or the sodium metal is added to the reaction device in the form of solid sodium metal, the solid sodium metal added to the reaction device is converted into liquid sodium metal by external heating, and reacts with the introduced ammonia gas. After the reaction generates reaction heat, the solid sodium metal subsequently added is converted into liquid sodium metal by the released reaction heat, and a heating device is provided on the outer surface of the reaction device.

9. The method according to any one of claims 1 to 6, wherein: It includes the start-up phase and the stable reaction phase; In the startup phase, metallic sodium is added to the reaction device, and the heating device is turned on to raise the temperature to 300-400° C. In the reaction device, ammonia enters the reaction material from the lower part of the reaction device. As the sodium amide liquid level in the reaction device gradually increases, the height of the ammonia gas entering the reaction material in the reaction device is adjusted accordingly. When the sodium amide liquid level reaches a preset height position, the startup phase is completed and the stable reaction phase begins. During the stable reaction stage, the reaction heat is used to maintain the reaction, the reaction temperature is controlled within the range of 300-400°C, and the sodium amide liquid level is kept relatively stable. The height at which ammonia enters the reaction material inside the reaction device is also relatively stable, above the upper half of the height of the sedimentation zone. During the stable reaction stage, the weight ratio of metallic sodium to ammonia is 1:0.74-1.

08.

10. A device for continuously synthesizing sodium amide according to the method of any one of claims 1 to 9, comprising a reaction unit, a liquid metal sodium storage device, a pump, a sodium amide storage device, and a jacket layer arranged outside the reaction unit; the pump is connected to the jacket layer, the liquid metal sodium storage device, and the reaction unit feeding port to pump liquid metal sodium between the jacket layer, the liquid metal sodium storage device, and the reaction unit; the sodium amide storage device is arranged outside the reaction unit, and the sodium amide storage device is connected to a sodium amide removal pipeline in the reaction unit; the reaction unit is provided with a feeding port, an air inlet assembly, and a gas discharge port, characterized in that The lower part of the reaction device is a sedimentation zone, the discharge position of sodium amide is set at the lower part of the sedimentation zone, and the outlet height position of the air inlet component in the reaction device is adjustable.

11. The device according to claim 10, wherein The air intake assembly includes an air intake pipe and a gas distributor connected to the air intake pipe. The portion of the air intake pipe in the reaction device extends from the upper part of the device to the lower part of the device. The length of the portion of the air intake pipe in the reaction device is telescopically adjustable.

12. The device according to claim 10, wherein The air intake assembly includes an air intake pipe and at least two gas distributors connected to the air intake pipe. The portion of the air intake pipe inside the reaction device extends from the upper part of the device to the lower part of the device. Each of the gas distributors is connected to the portion of the air intake pipe inside the reaction device and has a different height position on the air intake pipe.

13. The device according to claim 10, wherein The air intake assembly includes at least two air intake pipes and a gas distributor connected to each air intake pipe. The portion of each air intake pipe in the reaction device extends from the upper part of the device to the lower part of the device, and each gas distributor is at a different height position in the reaction device.

14. The device according to claim 10, wherein The air intake assembly includes three air intake pipes and a gas distributor connected to each air intake pipe. The three gas distributors are at different heights in the reaction device, and are respectively the first gas distributor, the second gas distributor and the third gas distributor from bottom to top according to their heights.

15. The device according to any one of claims 10 to 14, characterized in that The device further comprises a heating device arranged outside the reaction device.

16. The device according to any one of claims 10 to 14, characterized in that The device further comprises a temperature-lowering device arranged outside the reaction device.

17. The device according to any one of claims 10 to 14, characterized in that A discharge port is provided at the bottom of the reaction device body, and the sodium amide removal pipeline is connected to the discharge port.

18. The device according to any one of claims 10 to 14, characterized in that The sodium amide removal pipeline is inserted into the discharge position of the sedimentation zone.

19. The device according to any one of claims 10 to 14, characterized in that The device further comprises a tail gas treatment device connected to the gas discharge port of the reaction device.

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