Ammonification reaction device

Abstract

The utility model discloses an ammonification reaction device and relates to the technical field of chemical equipment. The ammoniation reaction device comprises a plurality of ammoniation reaction kettles, a gas inlet pipeline, a liquid inlet pipeline and a plurality of overflow pipelines, the plurality of ammoniation reaction kettles comprise a first ammoniation reaction kettle, a second ammoniation reaction kettle and a third ammoniation reaction kettle which are communicated in sequence, and the gas inlet pipeline comprises a main pipeline and a plurality of branch pipelines. Flow control valves are arranged on the plurality of branch pipelines, and the gas conveying ends of the plurality of branch pipelines are respectively communicated with the gas inlets of the plurality of ammonification reaction kettles, so that ammonia gas is respectively introduced into the plurality of ammonification reaction kettles; the liquid inlet pipeline is communicated with a liquid inlet of the first ammonification reaction kettle so as to introduce hydrochloric acid into the first ammonification reaction kettle. The ammonification reaction kettles are connected in series, and the ammonia gas introduction amount of different ammonification reaction kettles is controlled, so that the problem that ammonia gas and hydrochloric acid violently react in the reaction kettles can be solved, the reaction process is better controlled, and the reaction efficiency is improved.

Description

Technical Field

[0001] This utility model relates to the field of chemical equipment technology, and in particular to an ammoniation reaction device. Background Technology

[0002] Currently, a reaction vessel is required for the neutralization reaction in the production of ammonium chloride. However, existing reaction vessels often use hydrochloric acid and ammonia water for the reaction during the preparation of ammonium chloride, which leads to problems such as uneven material mixing, excessively high reaction temperature, and insufficient reaction time. As a result, the reaction vessel is not very effective, and the ammonium chloride reaction is incomplete, affecting the quality of ammonium chloride. Utility Model Content

[0003] The main purpose of this invention is to provide an ammoniation reaction apparatus, which aims to provide an ammoniation reaction apparatus that can make the neutralization reaction during ammonium chloride production more complete and have higher reaction efficiency.

[0004] To achieve the above objectives, the ammoniation reaction apparatus proposed in this utility model includes:

[0005] Multiple ammoniation reactors, including a first ammoniation reactor, a second ammoniation reactor, and a third ammoniation reactor connected in sequence, each ammoniation reactor including a reactor body and a liquid inlet, an air inlet, and a discharge outlet located on the reactor body and staggered;

[0006] An air intake pipe is provided, comprising a main pipe and multiple branch pipes. The main pipe is connected to the multiple branch pipes respectively. One end of the main pipe forms an air intake end, and the ends of each branch pipe away from the main pipe form air delivery ends. The air delivery ends of the multiple branch pipes are connected to the air inlets of multiple ammoniation reactors respectively, so as to introduce ammonia gas into the first ammoniation reactor, the second ammoniation reactor, and the third ammoniation reactor respectively through the main pipe and the multiple branch pipes. Each of the multiple branch pipes is equipped with a flow control valve.

[0007] A liquid inlet pipe, the liquid inlet pipe being connected to the liquid inlet of the first ammoniation reactor, for introducing hydrochloric acid into the first ammoniation reactor; and,

[0008] Multiple overflow pipes are arranged along the direction of the multiple ammoniation reactors, and each overflow pipe connects the outlet and inlet of two adjacent ammoniation reactors.

[0009] In this process, hydrochloric acid and ammonia gas introduced into the first ammoniation reactor react in the first ammoniation reactor. After the liquid level in the first ammoniation reactor reaches the discharge port height, it flows into the second ammoniation reactor through the overflow pipe and reacts with the introduced ammonia gas in the second ammoniation reactor. After the liquid level in the second ammoniation reactor reaches the discharge port height, it flows into the third ammoniation reactor through the overflow pipe and reacts with the introduced ammonia gas in the third ammoniation reactor before flowing out from the discharge port to obtain ammonium chloride.

[0010] In one embodiment, the first ammoniation reactor and the second ammoniation reactor are further provided with a reflux inlet at the upper end and a reflux outlet at the lower end.

[0011] The ammoniation reaction apparatus also includes multiple reflux pipes corresponding to the multiple ammoniation reactors, and each reflux pipe is connected to the reflux outlet and reflux inlet of the same ammoniation reactor.

[0012] In one embodiment, a heat exchanger is provided on the reflux pipe to exchange heat with the material flowing out of the reflux outlet and then return it to the corresponding ammoniation reactor through the reflux inlet.

[0013] In one embodiment, a circulation pump is provided on the return pipe.

[0014] In one embodiment, the ammoniation reaction apparatus further includes a plurality of porous tubes placed inside the ammoniation reactor and connected to the corresponding branch pipes. The surface of the porous tubes is provided with a plurality of gas delivery holes to allow gas from each branch pipe to be introduced into each of the ammoniation reactors.

[0015] In one embodiment, the porous pipe includes a main pipe extending vertically and a plurality of branch pipes communicating with the side of the main pipe and inclined, and each branch pipe is provided with a plurality of air supply holes.

[0016] In one embodiment, the porous tube is arranged in the vertical direction, the length of the porous tube inside the ammoniation reactor is d, and the height of the ammoniation reactor is D, then 2 / 3D < d < D.

[0017] In one embodiment, the air inlets are arranged in a gradually denser pattern from top to bottom.

[0018] In one embodiment, in the first ammoniation reactor, the liquid inlet is located on the side wall of the reactor body near the bottom; and / or,

[0019] The height of the bottom of the first ammoniation reactor, the second ammoniation reactor, and the third ammoniation reactor decreases sequentially in the vertical direction.

[0020] In one embodiment, multiple second amination reactors are provided to slow down the reaction rate.

[0021] In the technical solution provided by this utility model, the gas inlet pipe includes a main pipe and multiple branch pipes. All gaseous ammonia enters each ammoniation reactor through the main pipe and then through each branch pipe. The amount of gaseous ammonia entering each ammoniation reactor is controlled by control valves on the branch pipes. Hydrochloric acid enters the first ammoniation reactor through the liquid inlet pipe. The hydrochloric acid and ammonia gas introduced into the first ammoniation reactor react in the first ammoniation reactor. After the material in the first ammoniation reactor reaches a certain liquid level, it enters the second ammoniation reactor through the overflow pipe and reacts with the introduced ammonia gas in the second ammoniation reactor. After the material in the second ammoniation reactor reaches a certain liquid level, it enters the third ammoniation reactor through the overflow pipe and reacts with the introduced ammonia gas in the third ammoniation reactor before flowing out from the outlet to obtain ammonium chloride. Therefore, the ammoniation reaction device provided by this utility model can use gaseous ammonia gas to react with hydrochloric acid through multiple ammoniation reactors connected in series, making the reaction more thorough and efficient. Attached Figure Description

[0022] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on the structures shown in these drawings without creative effort.

[0023] Figure 1 A schematic diagram of an embodiment of the ammoniation reaction apparatus provided by this utility model;

[0024] Figure 2 A schematic diagram of the structure of the first ammoniation reactor in one embodiment of the ammoniation reaction apparatus provided by this utility model.

[0025] Explanation of icon numbers:

[0026] 100. Ammoniation reaction apparatus; 1. Ammoniation reactor; 11. First ammoniation reactor; 12. Second ammoniation reactor; 13. Third ammoniation reactor; 14. Liquid inlet; 15. Gas inlet; 16. Discharge outlet; 17. Reflux liquid inlet; 18. Reflux discharge outlet; 2. Gas inlet pipe; 21. Main pipe; 22. Branch pipe; 23. Flow control valve; 3. Liquid inlet pipe; 4. Overflow pipe; 5. Reflux pipe; 51. Heat exchanger; 52. Circulation pump; 6. Perforated pipe.

[0027] The realization of the purpose, functional features and advantages of this utility model will be further explained in conjunction with the embodiments and with reference to the accompanying drawings. Detailed Implementation

[0028] The technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only some embodiments of the present utility model, and not all embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the protection scope of the present utility model.

[0029] It should be noted that if the embodiments of this utility model involve directional indicators (such as up, down, left, right, front, back, etc.), the directional indicators are only used to explain the relative positional relationship and movement of the components in a certain specific posture (as shown in the figure). If the specific posture changes, the directional indicators will also change accordingly.

[0030] Furthermore, if the embodiments of this utility model involve descriptions such as "first" or "second," these descriptions are for descriptive purposes only and should not be construed as indicating or implying their relative importance or implicitly specifying the number of indicated technical features. Therefore, features defined with "first" or "second" may explicitly or implicitly include at least one of those features. Additionally, the technical solutions of the various embodiments can be combined with each other, but this must be based on the ability of those skilled in the art to implement them. If the combination of technical solutions is contradictory or impossible to implement, it should be considered that such a combination of technical solutions does not exist and is not within the scope of protection claimed by this utility model.

[0031] Currently, a reaction vessel is required for the neutralization reaction in the production of ammonium chloride. However, existing reaction vessels often use hydrochloric acid and ammonia water for the reaction during the preparation of ammonium chloride, which leads to problems such as uneven material mixing, excessively high reaction temperature, and insufficient reaction time. As a result, the reaction vessel is not very effective, and the ammonium chloride reaction is incomplete, affecting the quality of ammonium chloride.

[0032] To solve this technical problem, this utility model provides an amination reaction apparatus 100. Please refer to [link / reference]. Figure 1The ammoniation reaction apparatus 100 includes multiple ammoniation reactors 1, an inlet pipe 2, a liquid inlet pipe 3, and multiple overflow pipes 4. Each ammoniation reactor 1 includes a first ammoniation reactor 11, a second ammoniation reactor 12, and a third ammoniation reactor 13 connected in sequence. Each ammoniation reactor 1 includes a reactor body and a liquid inlet 14, an inlet 15, and a outlet 16 located on the reactor body and staggered. The inlet pipe 2 includes a main pipe 21 and multiple branch pipes 22. The main pipe 21 is connected to each of the branch pipes 22. One end of the main pipe 21 forms an inlet, and the ends of each branch pipe 22 away from the main pipe 21 form outlets. The outlets of the branch pipes 22 are connected to the inlets 15 of each of the ammoniation reactors 1, so that ammonia gas is introduced into the first ammoniation reactor 11, the second ammoniation reactor 12, and the third ammoniation reactor 13 respectively through the main pipe 21 and the branch pipes 22. The reactor 13 has flow control valves 23 on each of the branch pipes 22; the liquid inlet pipe 3 is connected to the liquid inlet 14 of the first ammoniation reactor 11 to introduce hydrochloric acid into the first ammoniation reactor 11; along the arrangement direction of the plurality of ammoniation reactors 1, each overflow pipe 4 is connected to the discharge port 16 and the liquid inlet 14 of two adjacent ammoniation reactors 1; wherein, the hydrochloric acid introduced into the first ammoniation reactor 11 and the ammonia gas introduced into the first ammoniation reactor 11 are... The reaction takes place in reactor 11. After the liquid level of the material in the first ammoniation reactor 11 reaches the height of the discharge port 16, it enters the second ammoniation reactor 12 through the overflow pipe 4 and reacts with the introduced ammonia gas in the second ammoniation reactor 12. After the liquid level of the material in the second ammoniation reactor 12 reaches the height of the discharge port 16, it enters the third ammoniation reactor 13 through the overflow pipe 4 and reacts with the introduced ammonia gas in the third ammoniation reactor 13 before flowing out from the discharge port 16 to obtain ammonium chloride.

[0033] In the technical solution provided by this utility model, the air inlet pipe 2 includes a main pipe 21 and multiple branch pipes 22. All gaseous ammonia enters each ammoniation reactor 1 through the main pipe 21 and then through each branch pipe 22. The amount of gaseous ammonia entering each ammoniation reactor 1 is controlled by the flow control valve 23 on the branch pipe 22. Hydrochloric acid enters the first ammoniation reactor 11 through the liquid inlet pipe 3. The hydrochloric acid and ammonia gas introduced into the first ammoniation reactor 11 react in the first ammoniation reactor 11. After the liquid level of the material in the first ammoniation reactor 11 reaches the height of the discharge port 16, it enters the second ammoniation reactor 12 through the overflow pipe 4 and reacts with the introduced ammonia gas in the second ammoniation reactor 12. After the liquid level of the material in the second ammoniation reactor 12 reaches the height of the discharge port 16, it enters the third ammoniation reactor 13 through the overflow pipe 4 and reacts with the introduced ammonia gas in the third ammoniation reactor 13 before flowing out from the discharge port 16 to obtain ammonium chloride. In this process, most of the ammonia gas is introduced into the first ammoniation reactor 11 or the second ammoniation reactor 12 to react with hydrochloric acid, while a small portion of the ammonia gas is introduced into the third ammoniation reactor 13 to make the reaction milder. Therefore, the ammoniation reaction device 100 provided by this utility model can use gaseous ammonia gas to react with hydrochloric acid through multiple ammoniation reactors 1 connected in series. On the one hand, it can reduce the sudden increase in pH or local over-alkaliness caused by excessive ammonia gas in a single reactor, thereby reducing the situation of violent reaction or increased side reactions. On the other hand, the heat released by the neutralization reaction is dispersed to multiple ammoniation reactors 1, reducing the temperature rise rate of a single reactor and reducing the decomposition of ammonium chloride or thermal stress on the equipment caused by high temperature. Therefore, it can not only make the reaction between ammonia gas and hydrochloric acid milder, but also make the reaction more efficient and thorough.

[0034] In some embodiments, the first ammoniation reactor 11 and the second ammoniation reactor 12 are further provided with a reflux inlet 17 at the upper end and a reflux outlet 18 at the lower end. The ammoniation reaction apparatus 100 also includes multiple reflux pipes 5 corresponding to the multiple ammoniation reactors 1, each reflux pipe 5 connecting the reflux outlet 18 and the reflux inlet 17 of the same ammoniation reactor 1. The material in the first ammoniation reactor 11 and / or the second ammoniation reactor 12 can be transported from the reflux outlet 18 at the lower end of the reactor body to the upper end of the reactor body via the corresponding reflux pipe 5 and the reflux inlet 17 at the upper end of the reactor body, thereby improving the mixing uniformity and increasing the reactant conversion rate.

[0035] In some embodiments, a heat exchanger 51 is provided on the reflux pipe 5 to cool the material flowing out of the reflux outlet 18 and then return it to the corresponding ammoniation reactor 1 via the reflux inlet 17. The heat exchanger 51 enables better control of the reaction temperature, reduces the generation of side reactions, and improves reaction efficiency.

[0036] To transport the reflux liquid from the reflux outlet 18 at the bottom of the reactor to the reflux inlet 17 at the top, a power unit is required. Therefore, in some embodiments, a circulation pump 52 is installed on the reflux pipe 5. The circulation pump 52 drives the reaction liquid to flow continuously, which solves the problems of uneven mixing and poor material flowability within the reactor, improves gas-liquid mass transfer efficiency, ensures sufficient contact between ammonia and hydrochloric acid, and increases the conversion rate.

[0037] In some embodiments, the ammoniation reaction apparatus 100 further includes a plurality of porous tubes 6, which are placed inside the ammoniation reactor 1 and connected to the corresponding branch pipes 22. The surface of each porous tube 6 is provided with a plurality of gas outlet holes to allow gas from each branch pipe 22 to be introduced into each of the ammoniation reactors 1. This arrangement allows ammonia gas to be more evenly dispersed in the reactor through the gas outlet holes of the porous tubes 6, which not only reduces the occurrence of side reactions caused by excessively high local pH, but also increases the contact area between ammonia gas and hydrochloric acid, thereby improving reaction efficiency.

[0038] In some embodiments, the porous tube 6 includes a main tube extending vertically and multiple branch tubes connected to the side of the main tube and arranged at an angle. Each branch tube is provided with multiple gas delivery holes. The multiple branch tubes arranged at an angle, together with the main tube extending vertically, form a three-dimensional distribution, allowing ammonia gas bubbles to cover different heights and radial areas of the reactor, further improving the gas-liquid contact efficiency, promoting the full reaction of ammonia and hydrochloric acid, and improving the reaction efficiency.

[0039] In some embodiments, the porous tube 6 is arranged vertically, and the length of the porous tube 6 inside the ammoniation reactor 1 is d, while the height of the ammoniation reactor 1 is D. Therefore, 2 / 3D < d < D. This arrangement optimizes the depth of gas distribution, thereby improving reaction uniformity and efficiency.

[0040] In some embodiments, the gas inlets are arranged with gradually increasing density from top to bottom. The high density of gas inlets at the lower end of the porous tube 6 can disperse the amount of ammonia gas introduced, preventing a concentrated release of ammonia gas that could cause a sudden increase in pH. In addition, there is more hydrochloric acid in the lower part of the reactor than in the upper part. This arrangement can deliver more ammonia gas to the area with more hydrochloric acid, thereby improving the efficiency of the reaction.

[0041] In some embodiments, in the first ammoniation reactor 11, the liquid inlet 14 is located on the side wall of the reactor body near the bottom, and the gas inlet 15 is located on the side wall of the reactor body near the top or at the top of the reactor. When hydrochloric acid enters the reactor from the bottom side wall, it can be pressurized and transported by a centrifugal pump or a metering pump. The kinetic energy provided by the pump overcomes gravity and fluid resistance, pushing the liquid (hydrochloric acid) upward. Meanwhile, the gas (gaseous ammonia) diffuses downward from the top. The countercurrent movement of the two prolongs the gas-liquid contact time. This countercurrent effect not only improves the gas-liquid mass transfer efficiency but also improves the ammonia utilization rate.

[0042] It should be noted that in each ammoniation reactor 1, the liquid inlet 14 can be located on the side wall of the reactor body near the bottom. The gas inlet 15 can be located on the side wall of the reactor body near the top or at the top of the reactor. The discharge outlet 16 can be located on the side wall of the reactor body near the top, with different heights determined according to different actual conditions. For example, to make the reaction more complete, the discharge outlet 16 can be set slightly higher; while in the case of multiple second ammoniation reactors 12, the discharge outlet 16 can be set slightly lower, and so on. It is understood that the height of the discharge outlet 16 of the previous ammoniation reactor 1 is higher than the height of the liquid inlet 14 of the next ammoniation reactor 1.

[0043] In some embodiments, the bottom of the bodies of the first ammoniation reactor 11, the second ammoniation reactor 12, and the third ammoniation reactor 13 decreases sequentially in the vertical direction. This is beneficial to increasing the height difference between the discharge port 16 of the previous ammoniation reactor 1 and the liquid inlet 14 of the next ammoniation reactor 1, thereby facilitating the smooth transfer of materials from the previous ammoniation reactor 1 to the next ammoniation reactor 1.

[0044] In some embodiments, multiple second ammoniation reactors 12 are provided, and these reactors are connected in series via the overflow pipe 4. Each second ammoniation reactor 12 independently adjusts the ammonia flow rate via a flow control valve 23 on the branch pipe 22, neutralizing hydrochloric acid (HCl) stage by stage. This further reduces the generation of ammonia byproducts caused by sudden pH increases in a single reactor, improving product purity and production efficiency. Furthermore, the staged flow of material through multiple reactors increases the reaction time, allowing for more thorough contact between ammonia and hydrochloric acid, thereby improving the conversion rate.

[0045] In the technical solution of this utility model, the amount of gaseous ammonia entering each of the ammoniation reactors 1 is controlled by the flow control valve 23. The gaseous ammonia entering each of the ammoniation reactors 1 is evenly distributed in the hydrochloric acid under the action of the porous tube 6 inside, so that the gaseous ammonia and hydrochloric acid are fully mixed. By connecting the reflux outlet 18 and the reflux inlet 17 of the same ammoniation reactor 1 through the reflux pipe 5, the reaction time of the material in a single reactor can be increased, so that the reaction is more complete. A circulation pump 52 and a heat exchanger 51 are set on each reflux pipe 5. The reactants in the ammoniation reactor 1 enter the circulation pump 52 for pressurization through the reflux pipe 5, and then return to the current ammoniation reactor 1 after being heated to a specific temperature by the heat exchanger 51. The heat exchange of the reactants by the heat exchanger 51 can accurately control the internal temperature of the ammoniation reactor 1. The circulation of the reactants by the circulation pump 52 can make the hydrochloric acid and ammonia mix more evenly. Through the above measures, the technical effects of uniform material mixing, accurate temperature control, higher reaction efficiency, and fewer by-products can be achieved.

[0046] The above description is merely an exemplary embodiment of the present utility model and does not limit the patent scope of the present utility model. Any equivalent structural transformations made based on the technical concept of the present utility model and the contents of the present utility model specification and drawings, or direct / indirect applications in other related technical fields, are included within the patent protection scope of the present utility model.

Claims

1. An ammoniation reaction apparatus, characterized in that, The ammoniation reaction apparatus includes: Multiple ammoniation reactors, including a first ammoniation reactor, a second ammoniation reactor, and a third ammoniation reactor connected in sequence, each ammoniation reactor including a reactor body and a liquid inlet, an air inlet, and a discharge outlet located on the reactor body and staggered; An air intake pipe is provided, comprising a main pipe and multiple branch pipes. The main pipe is connected to the multiple branch pipes respectively. One end of the main pipe forms an air intake end, and the ends of each branch pipe away from the main pipe form air delivery ends. The air delivery ends of the multiple branch pipes are connected to the air inlets of multiple ammoniation reactors respectively, so as to introduce ammonia gas into the first ammoniation reactor, the second ammoniation reactor, and the third ammoniation reactor respectively through the main pipe and the multiple branch pipes. Each of the multiple branch pipes is equipped with a flow control valve. A liquid inlet pipe, the liquid inlet pipe being connected to the liquid inlet of the first ammoniation reactor, for introducing hydrochloric acid into the first ammoniation reactor; and, Multiple overflow pipes are arranged along the direction of the multiple ammoniation reactors, and each overflow pipe connects the outlet and inlet of two adjacent ammoniation reactors. In this process, hydrochloric acid and ammonia gas introduced into the first ammoniation reactor react in the first ammoniation reactor. After the liquid level in the first ammoniation reactor reaches the discharge port height, it flows into the second ammoniation reactor through the overflow pipe and reacts with the introduced ammonia gas in the second ammoniation reactor. After the liquid level in the second ammoniation reactor reaches the discharge port height, it flows into the third ammoniation reactor through the overflow pipe and reacts with the introduced ammonia gas in the third ammoniation reactor before flowing out from the discharge port to obtain ammonium chloride.

2. The ammoniation reaction apparatus as described in claim 1, characterized in that, The first ammoniation reactor and the second ammoniation reactor are also provided with a reflux inlet at the upper end and a reflux outlet at the lower end. The ammoniation reaction apparatus also includes multiple reflux pipes corresponding to the multiple ammoniation reactors, and each reflux pipe is connected to the reflux outlet and reflux inlet of the same ammoniation reactor.

3. The ammoniation reaction apparatus as described in claim 2, characterized in that, The reflux pipe is equipped with a heat exchanger to exchange heat with the material flowing out of the reflux outlet and then return it to the corresponding ammoniation reactor through the reflux inlet.

4. The ammoniation reaction apparatus as described in claim 2, characterized in that, A circulation pump is installed on the return pipe.

5. The ammoniation reaction apparatus as described in claim 1, characterized in that, The ammoniation reaction apparatus further includes multiple porous tubes, which are placed inside the ammoniation reactor and connected to the corresponding branch pipes. The surface of the porous tubes is provided with multiple gas outlets to allow gas from each branch pipe to be introduced into each of the ammoniation reactors.

6. The ammoniation reaction apparatus as described in claim 5, characterized in that, The porous pipe includes a main pipe extending vertically and multiple branch pipes connected to the side of the main pipe and inclined, and each branch pipe is provided with multiple air delivery holes.

7. The ammoniation reaction apparatus as described in claim 6, characterized in that, The porous tube is arranged in the vertical direction. The length of the porous tube inside the ammoniation reactor is d, and the height of the ammoniation reactor is D. Then 2 / 3D < d < D.

8. The ammoniation reaction apparatus as described in claim 6, characterized in that, The air inlets are arranged in a gradually denser pattern from top to bottom.

9. The ammoniation reaction apparatus as described in claim 1, characterized in that, In the first amination reactor, the liquid inlet is located on the side wall of the reactor body near the bottom; and / or, The height of the bottom of the first ammoniation reactor, the second ammoniation reactor, and the third ammoniation reactor decreases sequentially in the vertical direction.

10. The ammoniation reaction apparatus as described in claim 1, characterized in that, Multiple second amination reactors are provided to slow down the reaction rate.

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