Deuterated ammonia production device

Abstract

Provided is a deuterated ammonia production device with which deuterated ammonia can be economically and efficiently produced by means of a flow system without requiring a catalyst or a post-stage separation process caused by the supply of a large amount of a carrier gas.　One aspect of the present invention is a deuterated ammonia production device comprising an absorption tower section composed of one or more stages of absorption towers, wherein: the absorption tower section has a filling material part composed of a filling material, an ammonia gas introduction part for introducing ammonia gas, a deuterated solvent introduction part for introducing a deuterated solvent, a deuterated ammonia gas discharge part for discharging deuterated ammonia gas, and a deuterated solvent discharge part for discharging a depleted deuterated solvent; and in the absorption tower section, the ammonia gas flows upward in the filling material part while the deuterated solvent flows downward in the filling material part, whereby absorption of the ammonia gas into the deuterated solvent and an isotope exchange reaction are performed in the filling material part to generate the deuterated ammonia gas.

Description

Deuterated ammonia production apparatus

[0001] The present invention relates to a deuterated ammonia production apparatus.

[0002] Deuterium is one of the stable isotopes of hydrogen, and it is known that a large isotope effect can be obtained because its mass difference is twice. For example, by substituting hydrogen atoms in a certain compound with deuterium, effects such as increased lifespan and durability can be obtained for substances composed of that compound. Therefore, in recent years, deuterium has been used in various fields such as pharmaceuticals, semiconductors, and organic EL. Deuterated ammonia is obtained by substituting hydrogen in ammonia molecules with deuterium. In the semiconductor field, for example, in the production of gigabyte DRAM, it is used as a source or reservoir of deuterium in the passivation films of silicon nitride and silicon oxynitride.

[0003] U.S. Patent No. 3,471,2,57, Japanese Patent Application Laid-Open No. 2023-177,916

[0004] B. M. Andreev, E.P. Magomedbekov, A. A. Raitman, M. B. Pozenkevich, Yu. A. Sakharovsky, A.V. Khoroshilov: Separation of isotopes of biogenic elements in two-phase systems, ELSEVIER

[0005] Isotope exchange can be used for the deuteration of ammonia. In Patent Document 1, isotope exchange is caused by contacting liquid ammonia and gaseous deuterium in an isotope exchange column to deuterate ammonia. However, according to Non-Patent Document 1, a catalyst is required for the isotope exchange reaction between liquid ammonia and gaseous deuterium, and potassium amide is generally used as the catalyst. Potassium amide is corrosive and is known to deteriorate the sealing material. In addition, cyanide is by-produced in the process of the isotope exchange reaction between liquid ammonia and gaseous deuterium, so waste liquid treatment is required. For the above reasons, there are engineering difficulties in the production of deuterated ammonia by the technique described in Patent Document 1.

[0006] Patent Document 2 describes an isotope exchange reaction carried out by mixing ammonia gas with a deuterated solvent. Specifically, a deuterated solvent having proton-exchangeable functional groups such as hydroxyl groups and amino groups is mixed and dissolved with undeuterated ammonia gas to carry out the exchange reaction, and then a carrier gas is supplied to extract the deuterated ammonia dissolved in the deuterated solvent in gaseous form. Although the technology described in Patent Document 2 does not require catalysts or wastewater treatment as described above, the problem is that the reaction itself is a batch process rather than a flow process, and a carrier gas is required to extract the deuterated ammonia.

[0007] The former arises because, as the reaction progresses, the deuterium concentration in the deuterated solvent decreases, requiring the deuterated solvent to be replaced after a certain amount of reaction has been completed. In batch processes, this reduces production efficiency due to the need to replace the deuterated solvent. The latter arises because, in order to reduce the frequency of replacement, a large amount of deuterated solvent is used, resulting in a large amount of ammonia dissolving in the deuterated solvent. Extracting deuterated ammonia requires a large amount of carrier gas, and since the carrier gas is a fluid other than ammonia, it needs to be separated in a later process, reducing the overall economic efficiency of the production process.

[0008] Therefore, the object of the present invention is to provide a deuterium ammonia production apparatus that enables economical and efficient production of deuterium ammonia in a flow manner, without requiring a subsequent separation process that involves the supply of catalysts or large amounts of carrier gas.

[0009] One aspect of the present invention is as follows:

[0010] [1] A deuterated ammonia production apparatus having an absorption tower section consisting of one or more absorption towers, wherein the absorption tower section comprises a packing section consisting of packing material provided at one or more locations within the absorption tower section, an ammonia gas introduction section for introducing ammonia gas into the absorption tower section, a deuterated solvent introduction section for introducing a deuterated solvent into the absorption tower section, a deuterated ammonia gas discharge section for discharging deuterated ammonia gas from within the absorption tower section, and a depleted deuterated solvent discharge section for discharging a depleted deuterated solvent, which is the deuterated solvent in which the ammonia gas has dissolved and the deuterium concentration has been reduced, wherein within the absorption tower section, the deuterated solvent flows downward through the packing section while the ammonia gas flows upward through the packing section, thereby causing the absorption of the ammonia gas into the deuterated solvent and an isotope exchange reaction to occur within the packing section, thereby producing deuterated ammonia gas.

[0011] [2] The deuterated ammonia production apparatus according to [1], wherein the absorption tower section, when consisting of one stage absorption tower, has the ammonia gas inlet and the deuterated solvent outlet at the bottom of the tower and the deuterated solvent inlet and the deuterated ammonia gas outlet at the top of the tower, and when consisting of two or more stages absorption towers, has the ammonia gas inlet and the deuterated solvent outlet at the bottom of the first stage absorption tower and the deuterated solvent inlet and the deuterated ammonia gas outlet at the top of the final stage absorption tower.

[0012] [3] The deuterated ammonia production apparatus according to [1] or [2], comprising: a heat exchanger that cools the deuterated ammonia gas discharged through the deuterated ammonia gas discharge section to liquefy the deuterated solvent in the deuterated ammonia gas; and a gas-liquid separator that separates the deuterated solvent liquefied by the heat exchanger from the deuterated ammonia gas.

[0013] [4] The deuterated ammonia production apparatus according to [3], wherein the absorption tower section has a deuterated solvent return section that returns the deuterated solvent separated by the gas-liquid separator to the absorption tower section.

[0014] [5] The deuterated ammonia production apparatus according to [4], wherein in the absorption tower section, the deuterated solvent introduction section, the packing material, and the deuterated solvent return section are arranged in this order toward the downstream side in the direction of flow of the deuterated solvent.

[0015] [6] A deuterated ammonia production apparatus according to any one of [1] to [5], further comprising a deuterated solvent heating device that heats the deuterated solvent discharged from the deuterated solvent discharge unit to desorb ammonia from the deuterated solvent and separate it from the deuterated solvent.

[0016] [7] The deuterated ammonia production apparatus according to [6], wherein the deuterated deuterated solvent heating apparatus comprises a storage tank for storing the deuterated deuterated solvent and a heating device for heating the deuterated deuterated solvent in the storage tank, and the storage tank comprises an introduction section for introducing the deuterated deuterated solvent into the storage tank, an discharge section for discharging the deuterated deuterated solvent from the storage tank and an ammonia discharge section for discharging the ammonia detached from the storage tank.

[0017] [8] The deuterated ammonia production apparatus according to [6] or [7], wherein the absorption tower section has an ammonia gas return section that returns the ammonia desorbed by the depletion deuterated solvent heating device to the absorption tower section.

[0018] [9] The deuterated ammonia production apparatus according to [8], wherein in the absorption tower section, the ammonia gas introduction section, the packing material, and the ammonia gas return section are arranged in this order toward the downstream side in the direction of ammonia gas flow.

[0019]

[10] A deuterated ammonia production apparatus according to any one of [1] to [9], further comprising an ammonia gas heating device for heating the ammonia gas flowing toward the ammonia gas introduction section.

[0020]

[11] The deuterated ammonia production apparatus according to any one of [1] to

[10] , wherein the absorption tower section has an operating pressure of 100 kPaA or more and less than 400 kPaA and an operating temperature of 20°C or more and less than 140°C.

[0021]

[12] A method for producing a deuterated ammonia product using a deuterated ammonia production apparatus described in any one of [1] to

[11] , wherein the deuterated ammonia product is produced using the deuterated ammonia gas discharged from the deuterated ammonia gas discharge section.

[0022] According to the present invention, it is possible to provide a deuterium ammonia production apparatus that enables economical and efficient production of deuterium ammonia in a flow manner, without requiring a subsequent separation process that involves the supply of catalysts or large amounts of carrier gas.

[0023] This is a schematic diagram showing a deuterated ammonia production apparatus according to the first embodiment of the present invention. This is a schematic diagram showing a modified example of the deuterated ammonia production apparatus shown in Figure 1. This is a schematic diagram showing a deuterated ammonia production apparatus according to the second embodiment of the present invention. This is a schematic diagram showing a deuterated ammonia production apparatus according to the third embodiment of the present invention. This is a schematic diagram showing a deuterated ammonia production apparatus according to an example of the present invention.

[0024] Hereinafter, embodiments of the present invention will be described with reference to the drawings.

[0025] As shown in Figure 1, in the first embodiment of the present invention, the deuterated ammonia production apparatus 1 has an absorption tower section 2 consisting of one or more absorption towers 2a (one stage in the example shown in Figure 1), and the absorption tower section 2 has a packing section 2b consisting of packing material provided in one or more locations within the absorption tower section 2, and ammonia gas (NH) inside the absorption tower section 2 ３ The ammonia gas introduction section 2c introduces ) into the absorption tower section 2, the deuterated solvent introduction section 2d introduces the deuterated solvent in liquid state into the absorption tower section 2, and deuterated ammonia gas (ND ３The absorption tower section 2 has a deuterated ammonia gas discharge section 2e that discharges deuterated ammonia gas, and a deuterated solvent discharge section 2f that discharges depleted deuterated solvent, which is a deuterated solvent in which ammonia gas has dissolved and the deuterium concentration has been reduced, in a liquid state. In the absorption tower section 2, as the deuterated solvent flows downward through the packing section 2b and the ammonia gas flows upward through the packing section 2b, absorption (dissolution) of ammonia gas into the deuterated solvent and isotope exchange reactions occur in the packing section 2b, generating deuterated ammonia gas.

[0026] With this configuration, deuterated ammonia gas can be obtained by performing the absorption of ammonia gas into the deuterated solvent and the isotope exchange reaction (as well as the desorption of deuterated ammonia gas from the deuterated solvent) in the packing section 2b of the absorption tower section 2, for example, under absorption equilibrium conditions. Therefore, deuterated ammonia gas can be obtained without using the catalyst required in the technology described in Patent Document 1, and without using the carrier gas required in the technology described in Patent Document 2. Thus, a deuterated ammonia production apparatus 1 can be obtained that does not require a subsequent separation process caused by the supply of a catalyst or a large amount of carrier gas, and can produce deuterated ammonia economically and efficiently in a flow manner.

[0027] Deuterated solvents are solvents that produce ammonia deuterated gas through the absorption and isotope exchange reactions of ammonia gas, such as heavy water (D ２ O) is the case. When the deuterating solvent is heavy water, the depleting deuterating solvent is light water (H ２ It contains O). The packing material is not particularly limited as long as it produces the above reaction. The packing material may be a regular packing material or a random packing material.

[0028] The deuterated ammonia production apparatus 1 includes an ammonia gas supply path 3 for supplying ammonia gas to an ammonia gas introduction section 2c, a deuterated solvent supply path 4 for supplying deuterated solvent to a deuterated solvent introduction section 2d, a deuterated ammonia gas discharge path 5 for discharging deuterated ammonia gas from a deuterated ammonia gas discharge section 2e, and a deuterated solvent discharge path 6 for discharging depleted deuterated solvent from a deuterated solvent discharge section 2f. The ammonia gas supply path 3 has an ammonia gas control valve 3a for adjusting the flow rate of ammonia gas. The deuterated solvent supply path 4 has a deuterated solvent control valve 4a for adjusting the flow rate of deuterated solvent.

[0029] In the example shown in Figure 1, the absorption tower section 2 consists of a single-stage absorption tower 2a, with an ammonia gas inlet 2c and a deuterated solvent outlet 2f at the bottom 2g of the tower, and a deuterated solvent inlet 2d and a deuterated ammonia gas outlet 2e at the top 2h of the tower. With this configuration, the absorption equilibrium layer that can be used for isotope exchange reactions can be made longer, thereby improving the reaction rate within the absorption tower section 2.

[0030] The absorption tower section 2 may consist of two or more absorption towers 2a (two stages in the example shown in Figure 2), as shown in the modified example in Figure 2. The ammonia gas introduction section 2c and the deuterated solvent discharge section 2f are located at the bottom 2g of the first stage absorption tower 2a, while the deuterated solvent introduction section 2d and the deuterated ammonia gas discharge section 2e are located at the top 2h of the final stage (second stage in this embodiment) absorption tower 2a. This configuration allows for a longer absorption equilibrium layer that can be used for isotope exchange reactions, thereby improving the reaction rate within the absorption tower section 2. Furthermore, even if there is a limit to the height of the absorption towers 2a, for example, an absorption tower section 2 with a desired length of flow path can be constructed by connecting a desired number of absorption towers 2a in series.

[0031] In this example, the connection section 2i connecting the preceding absorption tower 2a and the succeeding absorption tower 2a has a gas path 2i1 that sends gas from the top 2h of the preceding absorption tower 2a to the bottom 2g of the succeeding absorption tower 2a, and a liquid path 2i2 that sends liquid from the bottom 2g of the succeeding absorption tower 2a to the top 2h of the preceding absorption tower 2a. A pumping device or the like can be appropriately provided in the liquid path 2i2 to send the liquid upward.

[0032] The deuterated ammonia production apparatus 1 includes a heat exchanger 7 that liquefies the deuterated solvent in the deuterated ammonia gas by cooling the deuterated ammonia gas discharged through the deuterated ammonia gas discharge section 2e, and a gas-liquid separator 8 that separates the deuterated solvent liquefied by the heat exchanger 7 from the deuterated ammonia gas. With this configuration, the deuterated solvent can be efficiently separated from the deuterated ammonia gas.

[0033] The refrigerant for the heat exchanger 7 is not particularly limited and may be, for example, cooling water, fluorocarbon refrigerant, or organic solvent. In this embodiment, the heat exchanger 7 and the gas-liquid separator 8 are provided separately, but are not limited to this and may be configured as an integrated unit. When the deuterated solvent is heavy water, the temperature of the deuterated ammonia gas cooled by the heat exchanger 7 is preferably 4°C or higher and less than 30°C, and in particular, a lower temperature is more preferable from the viewpoint of reducing the amount of water vapor entrained.

[0034] The heat exchanger 7 and the gas-liquid separator 8 are installed in this order downstream on the deuterized ammonia gas discharge path 5. The deuterized ammonia gas discharge path 5 has an operating pressure regulating valve 5a downstream of the gas-liquid separator 8 to adjust the operating pressure of the absorption tower section 2.

[0035] The deuterated ammonia production apparatus 1 includes a deuterated solvent heating device 9 that heats the deuterated solvent discharged from the deuterated solvent discharge section 2f to desorb ammonia from the deuterated solvent and separate it from the deuterated solvent. With this configuration, the utilization efficiency of ammonia can be improved by appropriately utilizing the desorbed ammonia.

[0036] The depletion deuterated solvent heating device 9 comprises a storage tank 9a for storing the depletion deuterated solvent and a heating device 9b for heating the depletion deuterated solvent in the storage tank 9a. The storage tank 9a includes an introduction section 9a1 for introducing the depletion deuterated solvent into the storage tank 9a, an discharge section 9a2 for discharging the depletion deuterated solvent from the storage tank 9a, and an ammonia discharge section 9a3 for discharging the ammonia desorbed from the storage tank 9a. With this configuration, ammonia can be efficiently desorbed from the depletion deuterated solvent.

[0037] In this embodiment, the heating device 9b is composed of an electric heater, but it is not limited to this, and may be configured to heat using a heating fluid such as steam, for example. When the deuterated solvent is heavy water, it is preferable to adjust the temperature of the depleted deuterated solvent in the storage tank 9a to 20°C or higher and less than 140°C.

[0038] The storage tank 9a is located on the deuterated solvent discharge path 6. The deuterated solvent discharge path 6 has a liquid level adjustment valve 6a downstream of the discharge section 9a2 of the storage tank 9a, which discharges the depleted deuterated solvent containing dissolved ammonia gas while maintaining a constant liquid level in the storage tank 9a.

[0039] The absorption tower section 2 has an operating pressure of 100 kPaA or more and less than 400 kPaA, and an operating temperature of 20°C or more and less than 140°C. The operating pressure is adjusted by the operating pressure regulating valve 5a described above. This configuration enables efficient operation. The operating temperature is adjusted by a thermometer 10 that measures the temperature inside the absorption tower section 2, and a temperature control device 11 that adjusts the temperature inside the absorption tower section 2 based on the measurement results from the thermometer 10.

[0040] The ammonia gas control valve 3a, the deuterated solvent control valve 4a, the operating pressure control valve 5a, the heating device 9b, the liquid level control valve 6a, and the temperature control device 11 are controlled by a control device (not shown) which is composed of a computer or the like.

[0041] The deuterized ammonia production apparatus 1 produces a deuterized ammonia product using the deuterized ammonia gas discharged from the deuterized ammonia gas discharge section 2e. The deuterized ammonia production apparatus 1 may be configured to use the deuterized ammonia gas discharged from the deuterized ammonia gas discharge section 2e as is to produce the product, or it may be configured to have a post-processing section (not shown) that performs further processing as needed to produce deuterized ammonia gas as a product. The post-processing section may include a dehumidifying device (not shown) such as an adsorption purifier or a membrane purifier.

[0042] As in the second embodiment of the present invention shown in FIG. 3, the absorption tower section 2 may be configured to have a deuterated solvent return section 2j that returns the deuterated solvent separated by the gas-liquid separator 8 to the absorption tower section 2. According to this configuration, the utilization efficiency of the deuterated solvent can be improved.

[0043] As in this embodiment, the deuterated ammonia production apparatus 1 preferably has a configuration in which, in the absorption tower section 2, in the flow direction of the deuterated solvent, the deuterated solvent introduction section 2d, the packing, and the deuterated solvent return section 2j are positioned in this order toward the downstream side. According to this configuration, when returning the deuterated solvent, the loss gradient of the deuterated solvent in the absorption tower section 2 can be stabilized and the reaction efficiency in the absorption tower section 2 can be improved.

[0044] As in this embodiment, the absorption tower section 2 may be configured to have an ammonia gas return section 2k that returns the ammonia desorbed by the loss deuterated solvent heating device 9 to the absorption tower section 2. According to this configuration, the utilization efficiency of ammonia can be improved.

[0045] As in this embodiment, the deuterated ammonia production apparatus 1 preferably has a configuration in which, in the absorption tower section 2, in the flow direction of the ammonia gas, the ammonia gas introduction section 2c, the packing, and the ammonia gas return section 2k are positioned in this order toward the downstream side. According to this configuration, when returning the ammonia gas, the deuterium concentration gradient of the ammonia gas in the absorption tower section 2 can be stabilized and the reaction efficiency in the absorption tower section 2 can be improved. However, the ammonia gas introduction section 2c and the ammonia gas return section 2k may be configured to be shared. In this case, the ammonia gas introduction section 2c (ammonia gas return section 2k) may be configured to supply the ammonia gas blown into and supplied in the liquid in the storage tank 9a together with the ammonia gas desorbed from the liquid into the absorption tower section 2.

[0046] As in the third embodiment of the present invention shown in FIG. 4, the deuterated ammonia production apparatus 1 may be configured to include an ammonia gas heating device 12 that heats the ammonia gas flowing toward the ammonia gas introduction part 2c. According to this configuration, by raising the temperature of the peripheral part of the deuterated solvent discharge part 2f with the heated ammonia gas, the concentration of the ammonia gas dissolved in the deteriorated deuterated solvent in the peripheral part can be reduced, so that the utilization efficiency of ammonia can be improved. This effect is particularly effective when there is a liquid reservoir part 13 in which the deteriorated deuterated solvent accumulates in the peripheral part (inside the absorption tower part 2) as in this embodiment, but is not limited thereto. The deuterated ammonia production apparatus 1 may be configured to include a deteriorated deuterated solvent temperature raising device 9 in addition to the ammonia gas heating device 12.

[0047] Although the embodiments of the present invention have been described above, the present invention is not limited to the above-described embodiments, and the above-described embodiments can be variously modified without departing from the gist of the present invention.

[0048] As an example of the present invention, the deuterated ammonia production apparatus 1 shown in FIG. 5 was fabricated to produce deuterated ammonia. Deuterated solvent used was heavy water with a deuterium concentration of 99.8%. The packing used was DIXON Packing as random packing. The temperature adjustment device 11 used a cooling water circulation device to adjust so that the operating temperature of the absorption tower part 2 would be constant at 25°C. The heat exchanger 7 used a shell & tube type heat exchanger, and cooling water was used as the refrigerant.

[0049] In this embodiment, the deuterated ammonia production apparatus 1 was operated according to the following procedure: 1. A certain amount of heavy water was stored in the storage tank 9a, and ammonia gas was supplied from the ammonia gas inlet 2c until the ammonia concentration of the heavy water in the storage tank 9a reached the saturation concentration. 2. The power to the heating device 9b in the storage tank 9a was turned on, and heating was performed while controlling the temperature of the liquid in the storage tank 9a to a constant 85°C. Cooling water set to 15°C was also supplied to the heat exchanger 7. At this time, the set pressure of the operating pressure regulating valve 5a was set to 50 kPaG. 3. Once the temperature of each part was stable, the flow rate regulating valve of the ammonia gas inlet 2c was adjusted to start the supply of ammonia gas at a constant rate of 20 NL / min. At the same time, the flow rate regulating valve of the deuterated solvent inlet 2d was adjusted to start the supply of heavy water at a constant rate of 30 mL / min. Furthermore, control of the liquid level adjustment valve 6a was initiated, and the discharge of deuterated ammonia gas from the deuterated ammonia gas discharge section 2e of the absorption tower section 2 via the operating pressure adjustment valve 5a was initiated, and the discharge of depleted heavy water containing light water from the deuterated solvent discharge section 2f of the absorption tower section 2 via the liquid level adjustment valve 6a was initiated.

[0050] After the start of operation, once the operation of the deuterated ammonia production apparatus 1 was stable, the deuterated ammonia gas that would become the product was collected and analyzed for deuterium concentration, which was found to be 99%. The product flow rate at this time was 17 NL / min.

[0051] 1. Deuterated Ammonia Production Apparatus 2. Absorption Tower Section 2a. Absorption Tower 2b. Packing Section 2c. Ammonia Gas Inlet Section 2d. Deuterated Solvent Inlet Section 2e. Deuterated Ammonia Gas Outlet Section 2f. Deuterated Solvent Outlet Section 2g. Tower Bottom Section 2h. Tower Top Section 2i. Connection Section 2i1. Gas Path 2i2. Liquid Path 2j. Deuterated Solvent Return Section 2k. Ammonia Gas Return Section 3. Ammonia Gas Supply Path 3a. Ammonia Gas Control Valve 4. Deuterated Solvent Supply Path 4a. Deuterated Solvent Control Valve 5. Deuterated Ammonia Gas Outlet Path 5a. Operating Pressure Control Valve 6. Deuterated Solvent Outlet Path 6a. Liquid Level Control Valve 7. Heat Exchanger 8. Gas-Liquid Separator 9. Depletion Deuterated Solvent Heating Device 9a. Storage Tank 9a1. Inlet Section 9a2. Outlet Section 9a3. Ammonia Outlet Section 9b Heating device 10 Thermometer 11 Temperature control device 12 Ammonia gas heating device 13 Liquid reservoir

Claims

1. A deuterated ammonia production apparatus having an absorption tower section consisting of one or more absorption towers, wherein the absorption tower section comprises a packing section consisting of packing material provided at one or more locations within the absorption tower section, an ammonia gas introduction section for introducing ammonia gas into the absorption tower section, a deuterated solvent introduction section for introducing a deuterated solvent into the absorption tower section, a deuterated ammonia gas discharge section for discharging deuterated ammonia gas from within the absorption tower section, and a depleted deuterated solvent discharge section for discharging deuterated solvent, which is the deuterated solvent in which the ammonia gas has dissolved and the deuterium concentration has been reduced, wherein within the absorption tower section, the deuterated solvent flows downward through the packing section while the ammonia gas flows upward through the packing section, thereby causing the absorption of ammonia gas into the deuterated solvent and an isotope exchange reaction to occur within the packing section, thereby producing deuterated ammonia gas.

2. The deuterated ammonia production apparatus according to claim 1, wherein, when the absorption tower section consists of one stage, the ammonia gas inlet and the deuterated solvent outlet are located at the bottom of the tower, and the deuterated solvent inlet and the deuterated ammonia gas outlet are located at the top of the tower; and when the absorption tower section consists of two or more stages, the ammonia gas inlet and the deuterated solvent outlet are located at the bottom of the first stage of the absorption tower, and the deuterated solvent inlet and the deuterated ammonia gas outlet are located at the top of the final stage of the absorption tower.

3. The deuterated ammonia production apparatus according to claim 1, comprising: a heat exchanger that cools the deuterated ammonia gas discharged through the deuterated ammonia gas discharge section to liquefy the deuterated solvent in the deuterated ammonia gas; and a gas-liquid separator that separates the deuterated solvent liquefied by the heat exchanger from the deuterated ammonia gas.

4. The apparatus for producing deuterated ammonia according to claim 3, wherein the absorption tower section has a deuterated solvent return section that returns the deuterated solvent separated by the gas-liquid separator to the absorption tower section.

5. The deuterated ammonia production apparatus according to claim 4, wherein, in the absorption tower section, the deuterated solvent introduction section, the packing material, and the deuterated solvent return section are positioned in this order toward the downstream side in the flow direction of the deuterated solvent.

6. The apparatus for producing deuterated ammonia according to claim 1, further comprising a deuterated solvent heating device for heating the deuterated deuterated solvent discharged from the deuterated solvent discharge unit to desorb ammonia from the deuterated deuterated solvent and separate it from the deuterated deuterated solvent.

7. The deuterated ammonia production apparatus according to claim 6, wherein the deuterated deuterated solvent heating apparatus comprises a storage tank for storing the deuterated deuterated solvent and a heating device for heating the deuterated deuterated solvent in the storage tank, and the storage tank comprises an introduction section for introducing the deuterated deuterated solvent into the storage tank, an discharge section for discharging the deuterated deuterated solvent from the storage tank, and an ammonia discharge section for discharging the ammonia detached from the storage tank.

8. The deuterated ammonia production apparatus according to claim 6, wherein the absorption tower section has an ammonia gas return section that returns the ammonia desorbed by the depletion deuterated solvent heating device to the absorption tower section.

9. The deuterated ammonia production apparatus according to claim 8, wherein, in the absorption tower section, the ammonia gas introduction section, the packing material, and the ammonia gas return section are arranged in this order toward the downstream side in the direction of ammonia gas flow.

10. The deuterated ammonia production apparatus according to claim 1, further comprising an ammonia gas heating device for heating the ammonia gas flowing toward the ammonia gas introduction section.

11. The deuterated ammonia production apparatus according to claim 1, wherein the absorption tower section has an operating pressure of 100 kPaA or more and less than 400 kPaA, and an operating temperature of 20°C or more and less than 140°C.

12. A method for producing a deuterated ammonia product using the deuterated ammonia production apparatus described in claim 1, wherein the deuterated ammonia product is produced using the deuterated ammonia gas discharged from the deuterated ammonia gas discharge section.

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