Ammonia deuterated production equipment

Abstract

This invention provides a deuterium ammonia production apparatus that enables economical and efficient production of deuterium ammonia using a flow system, without requiring a subsequent separation process that involves the supply of catalysts or large amounts of carrier gas. [Solution] A deuterated ammonia production apparatus having an absorption tower section consisting of one or more stages, the absorption tower section comprising a packing section consisting of packing material, an ammonia gas introduction section for introducing ammonia gas, a deuterated solvent introduction section for introducing a deuterated solvent, a deuterated ammonia gas discharge section for discharging deuterated ammonia gas, and a deuterated solvent discharge section for discharging deuterated solvent, 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, producing deuterated ammonia gas.

Description

Technical Field

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

Background Art

[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 ELs. 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.

Prior Art Documents

Patent Documents

[0003]

Patent Document 1

Patent Document 2

Non-Patent Documents

[0004]

Non-Patent Document 1

Summary of the Invention

Problems to be Solved by the Invention

[0005] Isotope exchange can be used to deuterate ammonia. In Patent Document 1, isotope exchange is induced by contacting liquefied ammonia with 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 liquefied ammonia and gaseous deuterium, and potassium amide is generally used as the catalyst. Potassium amide is corrosive and is known to degrade sealing materials. In addition, cyanide is produced as a by-product in the isotope exchange reaction process between liquefied ammonia and gaseous deuterium, so wastewater treatment is necessary. For the reasons above, the production of deuterated ammonia using the technology described in Patent Document 1 is accompanied by engineering difficulties.

[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. [Means for solving the problem]

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

[0010] [1] It has an absorption tower section consisting of one or more absorption towers, The absorption tower section comprises a packing section consisting of packing material provided in 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 deuterated solvent discharge section for discharging depleted deuterated solvent, which is the deuterated solvent in which the ammonia gas has dissolved and the deuterium concentration has been reduced, from within the absorption tower section. A deuterated ammonia production apparatus, wherein in the absorption tower section, the deuterated solvent flows downward through the packed material section while the ammonia gas flows upward through the packed material section, thereby facilitating the absorption of the ammonia gas into the deuterated solvent and an isotope exchange reaction within the packed material section, 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 has the deuterated solvent inlet and the deuterated ammonia gas outlet at the top of the final stage absorption tower.

[0012] [3] 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, The apparatus for producing deuterated ammonia according to [1] or [2], further comprising a gas-liquid separator for separating 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], comprising a depleted deuterated solvent heating device that heats the depleted deuterated solvent discharged from the deuterated solvent discharge unit to desorb ammonia from the depleted deuterated solvent and separate it from the depleted deuterated solvent.

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

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

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

[0019]

[10] The deuterated ammonia production apparatus according to any one of [1] to [9], having an ammonia gas heating device that heats the ammonia gas flowing toward the ammonia gas introduction section.

[0020]

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

[10] .

[0021]

[12] A method for producing deuterated ammonia, using the deuterated ammonia production apparatus according to any one of [1] to

[11] to produce a deuterated ammonia product, A method for producing deuterated ammonia, in which the deuterated ammonia product is produced by the deuterated ammonia gas discharged from the deuterated ammonia gas discharge section.

Advantages of the Invention

[0022] According to the present invention, it is possible to provide a deuterated ammonia production apparatus that does not require a subsequent separation process due to the supply of a catalyst or a large amount of carrier gas, and can produce deuterated ammonia economically and efficiently by a flow method.

Brief Description of the Drawings

[0023] [Figure 1]This is a schematic diagram showing a deuterated ammonia production apparatus according to the first embodiment of the present invention. [Figure 2] Figure 1 is a schematic diagram showing a modified example of the deuterated ammonia production apparatus. [Figure 3] This is a schematic diagram showing a deuterated ammonia production apparatus according to a second embodiment of the present invention. [Figure 4] This is a schematic diagram showing a deuterated ammonia production apparatus according to a third embodiment of the present invention. [Figure 5] This is a schematic diagram showing a deuterated ammonia production apparatus according to an embodiment of the present invention. [Modes for carrying out the 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 (one stage in the example shown in Figure 1) absorption towers 2a, the absorption tower section 2 consists of a packing section 2b consisting of packing material provided at one or more locations within the absorption tower section 2, an ammonia gas introduction section 2c for introducing ammonia gas (NH3) into the absorption tower section 2, a deuterated solvent introduction section 2d for introducing a deuterated solvent in a liquid state into the absorption tower section 2, and deuterated ammonia gas (ND3) from within the absorption tower section 2 The absorption tower has a deuterated ammonia gas discharge section 2e and a deuterated solvent discharge section 2f that discharges a deuterated solvent in liquid form, which is a deuterated solvent in which ammonia gas has dissolved and the deuterium concentration has decreased from within the absorption tower section 2. Within the absorption tower section 2, as the deuterated solvent flows downward through the packing section 2b and ammonia gas flows upward through the packing section 2b, absorption (dissolution) of ammonia gas into the deuterated solvent and isotope exchange reactions occur within 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] The deuterating solvent is a solvent that produces deuterated ammonia gas through the absorption and isotope exchange reactions of ammonia gas, and is, for example, heavy water (D2O). When the deuterating solvent is heavy water, the depleting deuterating solvent includes light water (H2O). The packing material is not particularly limited as long as it produces the above reaction. The packing material may be ordered or disordered.

[0028] The deuterated ammonia production apparatus 1 includes an ammonia gas supply path 3 for supplying ammonia gas to an ammonia gas inlet 2c, a deuterated solvent supply path 4 for supplying deuterated solvent to a deuterated solvent inlet 2d, a deuterated ammonia gas discharge path 5 for discharging deuterated ammonia gas from a deuterated ammonia gas discharge path 2e, and a deuterated solvent discharge path 6 for discharging depleted deuterated solvent from a deuterated solvent discharge path 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 located at the bottom 2g of the tower, and a deuterated solvent inlet 2d and a deuterated ammonia gas outlet 2e located at the top 2h of the tower. 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.

[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 cools the deuterated ammonia gas discharged through the deuterated ammonia gas discharge section 2e to liquefy the deuterated solvent in the deuterated ammonia gas, 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 is even 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) consisting 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 shown in Figure 3, in the second embodiment of the present invention, the absorption tower section 2 may be configured to include a deuterated solvent return section 2j that returns the deuterated solvent separated by the gas-liquid separator 8 to the absorption tower section 2. This configuration improves the utilization efficiency of the deuterated solvent.

[0043] In the deuterated ammonia production apparatus 1, as in this embodiment, it is preferable that the deuterated solvent introduction section 2d, the packing material, and the deuterated solvent return section 2j are positioned in this order toward the downstream side in the direction of flow of the deuterated solvent within the absorption tower section 2. With this configuration, the loss gradient of the deuterated solvent within the absorption tower section 2 can be stabilized when the deuterated solvent is returned, thereby improving the reaction efficiency within the absorption tower section 2.

[0044] The absorption tower section 2 may be configured to include an ammonia gas return section 2k that returns the ammonia desorbed by the depletion deuterated solvent heating device 9 to the absorption tower section 2, as in this embodiment. This configuration improves the utilization efficiency of ammonia.

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

[0046] As shown in the third embodiment of the present invention in Figure 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 section 2c. With this configuration, the temperature of the area surrounding the deuterated solvent discharge section 2f can be increased by the heated ammonia gas, thereby reducing the concentration of ammonia gas dissolved in the depleted deuterated solvent in that area, and thus improving the utilization efficiency of ammonia. This effect is particularly effective when there is a liquid reservoir 13 in the area surrounding the depleted deuterated solvent (inside the absorption tower section 2), as in this embodiment, but is not limited to this. The deuterated ammonia production apparatus 1 may also be configured to include a depleted deuterated solvent heating device 9 in addition to the ammonia gas heating device 12.

[0047] Although embodiments of the present invention have been described above, the present invention is not limited to the embodiments described above, and the embodiments described above can be modified in various ways without departing from the spirit of the present invention. [Examples]

[0048] As an embodiment of the present invention, a deuterated ammonia production apparatus 1 shown in Figure 5 was fabricated and deuterated ammonia was produced. Heavy water with a deuterium concentration of 99.8% was used as the deuterating solvent. DIXON Packing was used as the packing material. The temperature control device 11 used a cooling water circulation system to adjust the operating temperature of the absorption tower section 2 to a constant 25°C. A shell-and-tube type heat exchanger 7 was used, and cooling water was used as the refrigerant.

[0049] In this example, the deuterium 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 a saturation concentration. 2. The power to the heating device 9b in the storage tank 9a was turned on, and the liquid in the storage tank 9a was heated while controlling the temperature to maintain 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. With the temperature of each section stable, the flow rate control valve of the ammonia gas inlet section 2c was adjusted to start supplying ammonia gas at a constant rate of 20 NL / min. At the same time, the flow rate control valve of the deuterated solvent inlet section 2d was adjusted to start supplying heavy water at a constant rate of 30 mL / min. In addition, control of the liquid level control valve 6a was started, 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 control valve 5a was started, 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 control valve 6a was started.

[0050] After the start of operation, once the operation of the deuterated ammonia production apparatus 1 had stabilized, 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. [Explanation of Symbols]

[0051] 1. Deuterium Ammonia Production System 2. Absorption tower section 2a Absorption tower 2b Filling section 2c Ammonia gas inlet 2d Deuterated solvent introduction section 2e Deuterated ammonia gas discharge section 2f Deuterated Solvent Discharge Section 2g tower bottom 2h Tower top 2i connection 2i1 gas route 2i2 Liquid pathway 2j Deuterated Solvent Return Section 2k Ammonia Gas Return Section 3. Ammonia gas supply route 3a Ammonia gas regulating valve 4. Deuterated solvent supply route 4a Deuterated solvent regulating valve 5. Deuterized ammonia gas emission pathway 5a Operating pressure regulating valve 6. Deuterated solvent efflux pathway 6a Liquid level adjustment valve 7 Heat exchanger 8 Gas-liquid separator 9. Degradation deuterated solvent heating device 9a Storage tank 9a1 Introduction 9a2 Discharge section 9a3 Ammonia discharge section 9b Heating device 10 Thermometer 11 Temperature adjustment device 12 Ammonia gas heating device 13 Liquid reservoir

Claims

1. It has an absorption tower section consisting of one or more absorption towers, The absorption tower section comprises a packing section consisting of packing material provided in 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 deuterated solvent discharge section for discharging depleted deuterated solvent, which is the deuterated solvent in which the ammonia gas has dissolved and the deuterium concentration has decreased, from within the absorption tower section. A deuterated ammonia production apparatus, wherein in the absorption tower section, the deuterated solvent flows downward through the packed material section while the ammonia gas flows upward through the packed material section, thereby facilitating the absorption of the ammonia gas into the deuterated solvent and an isotope exchange reaction within the packed material section, producing deuterated ammonia gas.

2. The deuterated ammonia production apparatus according to claim 1, wherein the absorption tower section, when consisting of a single 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 absorption towers, has the ammonia gas inlet and the deuterated solvent outlet at the bottom of the first stage absorption tower, and has the deuterated solvent inlet and the deuterated ammonia gas outlet at the top of the final stage absorption tower.

3. 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, The deuterated ammonia production apparatus according to claim 1, further comprising a gas-liquid separator for separating 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 depleted deuterated solvent heating device for heating the depleted deuterated solvent discharged from the deuterated solvent discharge unit to desorb ammonia from the depleted deuterated solvent and separate it from the depleted deuterated solvent.

7. The degraded deuterated solvent heating apparatus comprises a storage tank for storing the degraded deuterated solvent and a heating device for heating the degraded deuterated solvent in the storage tank. The deuterated ammonia production apparatus according to claim 6, wherein the storage tank comprises an introduction section for introducing the depleted deuterated solvent into the storage tank, an discharge section for discharging the depleted deuterated solvent from the storage tank, and an ammonia discharge section for discharging the ammonia desorbed 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 ammonia deuterated product using the ammonia deuterated production apparatus described in claim 1, A method for producing ammonia deuterated, comprising producing the ammonia deuterated product using the ammonia deuterated gas discharged from the ammonia deuterated gas discharge section.

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