Adsorption regeneration production process and system and application thereof

Abstract

The invention provides an adsorption regeneration production process and system and application thereof. The production process comprises an adsorption process, a pressure reduction process, a thermal regeneration process, a product gas purging process and a pressurizing process. Medium gas thermal regeneration gas and product gas replacement are combined, and variable-pressure regeneration and variable-temperature regeneration processes are combined; the method comprises the following steps: regenerating a dehydration adsorbent by adopting hot nitrogen, purging an adsorber by adopting high-purity ammonia gas after thermal regeneration, and then realizing near-zero treatment of impurity gas in a vacuumizing manner after purging. The variable-pressure regeneration process is provided with a vacuumizing process, so that the content of impurity gas in the system is reduced.

Description

Technical Field

[0001] The invention belongs to the technical field of chemical processes, and in particular relates to an adsorption regeneration production process and system and applications thereof. Background Art

[0002] In the production process of high-purity ammonia for industrial ammonia production, an adsorption process is usually set up to remove some impurities. Since the adsorption process has a saturated regeneration cycle, the regeneration usually has a temperature and pressure change regeneration process. The temperature change process generally introduces hot carrier gas, and the adsorbent is completely regenerated by sufficient purge. In order to avoid the introduction of new trace impurities in the regeneration process, high-purity product gas is usually used as the hot carrier gas, which causes product consumption during the purge process and reduces the product yield.

[0003] At present, there are several different production processes for high-purity ammonia production, which can be roughly classified into: complete distillation type, filtration adsorption distillation type and complete filtration adsorption type. Compared with the three processes, the complete filtration adsorption type production process is relatively simple, but its production quality is relatively low at present, and the product quality is determined by the purifier; the process of production based on distillation is more complicated than the process of production based on purifier adsorption. The production process needs to control the process parameters to make the product meet the requirements, but the quality of production based on distillation will be more stable; the filtration adsorption distillation process combines the respective advantages of distillation and adsorption, and has certain advantages in the production process of high-purity ammonia. However, the high-purity ammonia adsorption regeneration process currently used basically uses purified product gas for regeneration to ensure the cleanliness of its system.

[0004] In addition to the process of regenerating the adsorbent using product gas as regeneration gas, which is commonly used in high-purity gas production processes, in other gas purification fields, the process of using a third gas (a third gas other than feed gas and product gas) as regeneration gas is also commonly used. For example, air purification in air separation units and crude hydrogen purification in liquid nitrogen washing units all use nitrogen as the hot regeneration gas.

[0005] The existing adsorption regeneration process includes pressure swing regeneration and temperature swing regeneration process, and is equipped with regeneration heater, molecular sieve adsorber and other equipment. The adsorption regeneration process is equipped with a sequential control program. However, the disadvantages of the existing technology are:

[0006] 1) Using product gas as hot regeneration gas causes product consumption during the purge process, reducing product yield;

[0007] 2) The use of a third gas as the thermal regeneration gas introduces impurity gases, which increases the difficulty of purifying the downstream high-purity gas, and the product purity is not easy to meet the requirements.

[0008] Therefore, there is an urgent need for a high-purity ammonia production process that can achieve complete regeneration, does not introduce impurities during the process, and improves product yield. Summary of the invention

[0009] In order to solve the above problems in the prior art, the present invention proposes an adsorption regeneration production process and system and its application. The process of the present invention combines the intermediate gas thermal regeneration with the product gas replacement, and the pressure change regeneration with the temperature change regeneration process to achieve complete regeneration without introducing impurities, which is beneficial to improve the product yield and enhance the economic efficiency.

[0010] In a first aspect, the present invention proposes an adsorption regeneration production process, which includes an adsorption process, a decompression process, a thermal regeneration process, a product gas purge process, and a pressurization process.

[0011] As a specific embodiment of the present invention, in the adsorption process, the water-containing raw gas enters the adsorber, the water is removed, and a high-purity product gas is obtained; the water-containing raw gas includes water-containing ammonia;

[0012] In the decompression process, the adsorbent is partially regenerated by decompression to prepare for the thermal regeneration process;

[0013] In the thermal regeneration process, the regeneration gas is heated and then enters the adsorber to be fully regenerated with the adsorbent; the regeneration gas includes nitrogen; nitrogen is selected as the regeneration gas because the impurity gas in nitrogen is easily separated from ammonia.

[0014] The product gas purge process replaces the hot regeneration gas in the adsorber with product gas; the purpose of the product gas purge is to reduce the impact of regeneration gas impurities on the product gas, while reducing the temperature in the system to provide a temperature environment for the next step of reduced pressure regeneration.

[0015] The decompression process discharges the product gas in the system and reduces the excessive concentration of impurity gases caused by incomplete purging.

[0016] In the pressurization process, the adsorber is pressurized with the product gas, and the regeneration is completed.

[0017] In a second aspect, the present invention provides an adsorption regeneration production system, which includes a heater, a buffer tank, an adsorber, and a pressure reducing device; the heater is used to heat the regeneration gas;

[0018] The buffer tank is used to store product gas;

[0019] The adsorber is used to absorb moisture in the water-containing raw gas;

[0020] Pressure reducing equipment is used to discharge product gas.

[0021] As a specific implementation of the present invention, the inlet and outlet of the heater are both provided with temperature control valves.

[0022] As a specific embodiment of the present invention, the adsorber includes a first adsorber and a second adsorber.

[0023] As a specific implementation of the present invention, the adsorber is connected to a water-containing raw gas pipeline, and a switch valve is provided on the pipeline.

[0024] As a specific implementation of the present invention, the adsorber is connected to the buffer tank pipeline via a product gas pipeline, and both the inlet and outlet are provided with switch valves.

[0025] As a specific implementation of the present invention, the adsorber is connected to a regeneration gas pipeline, and both the inlet and outlet are provided with switch valves.

[0026] As a specific embodiment of the present invention, the adsorber is connected to the pressure reducing device via a regeneration gas pipeline, a switch valve is provided on the pressure reducing device pipeline, and a regeneration gas outlet switch valve is also provided on the regeneration gas pipeline; and a pressure equalizing valve is provided on the product gas pipeline.

[0027] Specifically, the specific operation process of the adsorption regeneration production system provided by the present invention includes the following steps:

[0028] S1: Adsorption process, water-containing raw gas enters the adsorber, water is removed, and high-purity product gas is obtained; the water-containing raw gas includes water-containing ammonia; the first adsorber is in the adsorption stage, and the second adsorber is in the static stage;

[0029] S2: Decompression process, the adsorbent is partially regenerated by decompression, and after the pressure is reduced, it is ready for the thermal regeneration process; the first adsorber is the adsorption stage, and the second adsorber is the decompression stage.

[0030] S3: Hot nitrogen regeneration process, the regenerated nitrogen is heated and enters the adsorber to fully regenerate with the adsorbent; the first adsorber adsorption stage, the second adsorber hot nitrogen regeneration stage:

[0031] S4: high-purity product gas purge process, the purge process replaces the hot regeneration gas in the adsorber with high-purity product gas; the first adsorber adsorption stage, the second adsorber product gas purge stage.

[0032] S5: After purging, a decompression process is performed to discharge the high-purity ammonia in the system; the first adsorber is in the adsorption stage, and the second adsorber is in the decompression stage; the pressure in the second adsorber drops to a vacuum state.

[0033] S6: charging process, using high-purity product gas to charge the adsorber, and regeneration ends; the first adsorber adsorption stage, the second adsorber charging stage;

[0034] S7: After the pressures of the first adsorber and the second adsorber are equalized, the pressure equalizing valve is closed; at this time, the state is the same as that of step S1, the first adsorber is in the adsorption stage, and the second adsorber is stationary for use.

[0035] In a third aspect, the present invention provides application of the production process described in the first aspect or the production system described in the second aspect in the field of producing high-purity ammonia.

[0036] Compared with the prior art, the present invention has the following beneficial effects:

[0037] 1. The production process of the present invention combines intermediate gas thermal regeneration with product gas replacement, and combines pressure swing regeneration with temperature swing regeneration; that is, hot nitrogen is used to regenerate the dehydration adsorbent, and high-purity ammonia is used to purge the adsorber after thermal regeneration, and after purge, near-zero treatment of impurity gases is achieved by vacuuming.

[0038] 2. In the production process of the present invention, the pressure-switching regeneration process is provided with a vacuuming process to reduce the content of impurity gases in the system.

[0039] 3. The production process of the present invention can reduce the consumption of high-purity ammonia gas during regeneration, reduce the operating cost of the high-purity ammonia process, and the regeneration is more thorough, which helps to ensure the quality of the high-purity ammonia gas. BRIEF DESCRIPTION OF THE DRAWINGS

[0040] Figure 1 A schematic diagram of a production system and process provided by an embodiment of the present invention;

[0041] The equipment includes 1-first adsorber, 2-second adsorber, 3-heater; 4-pressure reducing device; 5-buffer tank;

[0042] The valves include: 6-regeneration nitrogen switch valve; 7-first adsorber high-purity ammonia backflush valve; 8-second adsorber high-purity ammonia backflush valve; 9-first adsorber aqueous ammonia inlet switch valve; 10-second adsorber aqueous ammonia inlet switch valve; 11-first adsorber high-purity ammonia outlet switch valve; 12-second adsorber high-purity ammonia outlet switch valve; 13-first adsorber regeneration nitrogen inlet switch valve; 14-second adsorber regeneration nitrogen inlet switch valve; 15-first adsorber regeneration nitrogen outlet switch valve; 16-second adsorber regeneration nitrogen outlet switch valve; 17-regeneration nitrogen discharge valve; 18-pressure reducing device inlet switch valve; 19-equalizing valve; 20-heater inlet temperature control valve; 21-heater outlet temperature control valve. DETAILED DESCRIPTION

[0043] The present invention will be further described below in conjunction with specific embodiments, but they do not constitute any limitation to the present invention.

[0044] Example 1

[0045] This embodiment provides an adsorption regeneration production system for producing high-purity ammonia, the raw gas is aqueous ammonia, the regeneration gas is nitrogen, and the product gas is high-purity ammonia. Figure 1 , the specific structure is as follows:

[0046] The adsorption regeneration production system includes a first adsorber 1, a second adsorber 2, a heater 3, a pressure reducing device 4, and a buffer tank 5;

[0047] The adsorber is used to absorb water in the aqueous ammonia gas; the adsorber includes a first adsorber 1 and a second adsorber 2. The two adsorbers are respectively connected to the aqueous ammonia gas pipeline of the raw gas, and the first adsorber aqueous ammonia gas inlet switch valve 9 and the second adsorber aqueous ammonia gas inlet switch valve 10 are respectively arranged on the two pipelines.

[0048] The high-purity ammonia product gas obtained after the adsorber completes adsorption is connected to the buffer tank pipeline through the product gas pipeline, and the buffer tank is used for storing high-purity ammonia; the first adsorber high-purity ammonia outlet switch valve 11 and the second adsorber high-purity ammonia outlet switch valve 12 are set on the product gas pipelines passing through the two adsorbers.

[0049] The high-purity ammonia gas also leads to two adsorbers through pipelines. At this time, the high-purity ammonia gas is used as a purge gas to purge the adsorbers. The product gas backflush pipeline is provided with a first adsorber high-purity ammonia backflush valve 7 and a first adsorber high-purity ammonia backflush valve 8, and a pressure equalizing valve 19 is provided on the high-purity ammonia pipeline.

[0050] The heater is used to heat the regenerated nitrogen; the heating heat source is steam, and the steam is passed into the heater to heat the pipeline of the regenerated nitrogen. The pipeline of the regenerated nitrogen is provided with a regenerated nitrogen switch valve 6, and the inlet and outlet of the heater are respectively provided with a heater inlet temperature control valve 20 and a heater outlet temperature control valve 21; the heated regenerated nitrogen is connected to the adsorber through the regenerated nitrogen pipeline, and the regenerated nitrogen inlet switch valve 13 of the first adsorber regenerated nitrogen inlet switch valve 14 of the second adsorber regenerated nitrogen inlet switch valve 14, the first adsorber regenerated nitrogen outlet switch valve 15, and the second adsorber regenerated nitrogen outlet switch valve 16 are provided for the regenerated nitrogen to enter and exit the adsorber. A pipeline is also provided for the regenerated nitrogen to directly recover the regenerated nitrogen without passing through the pressure reducing device through the first adsorber regeneration outlet switch valve 15 and the second adsorber regeneration outlet switch valve 16, and a regenerated nitrogen discharge valve 17 is provided.

[0051] The pressure reducing device is used to discharge the regenerated nitrogen from the adsorber; the adsorber is connected to the pressure reducing device via the regenerated nitrogen pipeline, and a pressure reducing device inlet switch valve 18 is provided at the inlet of the pressure reducing device;

[0052] Example 2

[0053] This embodiment provides a specific operation flow of the production system provided in Example 1. Figure 1 , the details are as follows:

[0054] S1: adsorption process, water-containing ammonia enters the adsorber, water is removed, and high-purity ammonia is obtained; the water-containing raw gas includes water-containing ammonia; the first adsorber 1 is in the adsorption stage, and the second adsorber 2 is in the static stage;

[0055] The valve control status is as follows: the regeneration nitrogen switch valve 6 is closed; the first adsorber high-purity ammonia backflush valve 7 and the first adsorber high-purity ammonia backflush valve 8 are closed; the first adsorber aqueous ammonia inlet switch valve 9 is opened; the second adsorber aqueous ammonia inlet switch valve 10 is closed; the first adsorber high-purity ammonia outlet switch valve 11 is opened; the second adsorber high-purity ammonia outlet switch valve 12 is closed; the first adsorber regeneration nitrogen inlet switch valve 13 is closed; the second adsorber regeneration nitrogen inlet switch valve 14 is closed; the first adsorber regeneration nitrogen outlet switch valve 15 is closed; the second adsorber regeneration nitrogen outlet switch valve 16 is closed; the regeneration nitrogen discharge valve 17 is closed; the pressure reducing device inlet switch valve 18 is closed; the pressure equalizing valve 19 is closed; the heater inlet temperature control valve 20 and the heater outlet temperature control valve 21 are automatically put into operation;

[0056] S2: Decompression process, the adsorbent is partially regenerated by decompression, and after the pressure is reduced, it is ready for the thermal regeneration process; the first adsorber 1 is the adsorption stage, and the second adsorber 2 is the decompression stage.

[0057] The valve control status is as follows: the regeneration nitrogen switch valve 6 is closed; the first adsorber high-purity ammonia backflush valve 7 and the first adsorber high-purity ammonia backflush valve 8 are closed; the first adsorber water-containing ammonia inlet switch valve 9 is opened; the second adsorber water-containing ammonia inlet switch valve 10 is closed; the first adsorber high-purity ammonia outlet switch valve 11 is opened; the second adsorber high-purity ammonia outlet switch valve 12 is closed; the first adsorber regeneration nitrogen inlet switch valve 13 is closed; the second adsorber regeneration nitrogen inlet switch valve 14 is closed; the first adsorber regeneration nitrogen outlet switch valve 15 is closed; the second adsorber regeneration nitrogen outlet switch valve 16 is closed; open the regeneration nitrogen discharge valve 17 to reduce the pressure of the second adsorber; the pressure reducing device inlet switch valve 18 is closed; the pressure equalizing valve 19 is closed; the heater inlet temperature control valve 20 and the heater outlet temperature control valve 21 are automatically put into operation;

[0058] S3: hot nitrogen regeneration process, the regenerated nitrogen is heated and enters the adsorber to fully regenerate with the adsorbent;

[0059] The first adsorber 1 is in the adsorption stage, and the second adsorber 2 is in the hot nitrogen regeneration stage:

[0060] The valve control status is as follows: open the regeneration nitrogen switch valve 6; the first adsorber high-purity ammonia backflush valve 7 and the first adsorber high-purity ammonia backflush valve 8 are closed; the first adsorber water-containing ammonia inlet switch valve 9 is opened; the second adsorber water-containing ammonia inlet switch valve 10 is closed; the first adsorber high-purity ammonia outlet switch valve 11 is opened; the second adsorber high-purity ammonia outlet switch valve 12 is closed; the first adsorber regeneration nitrogen inlet switch valve 13 is closed; the second adsorber regeneration nitrogen inlet switch valve 14 is opened; the first adsorber regeneration nitrogen outlet switch valve 15 is closed; the second adsorber regeneration nitrogen outlet switch valve 16 is opened; the regeneration nitrogen discharge valve 17 is opened; the pressure reducing device inlet switch valve 18 is closed; the pressure equalizing valve 19 is closed; the heater inlet temperature control valve 20 and the heater outlet temperature control valve 21 are automatically put into operation;

[0061] S4: high-purity ammonia purge process, the purge process replaces the hot regenerated nitrogen in the adsorber with high-purity ammonia; the first adsorber 1 is the adsorption stage, and the second adsorber 2 is the product gas purge stage.

[0062] The valve control status is as follows: close the regeneration nitrogen switch valve 6; the first adsorber high-purity ammonia backflush valve 7 is closed, and the first adsorber high-purity ammonia backflush valve 8 is opened; the first adsorber aqueous ammonia inlet switch valve 9 is opened; the second adsorber aqueous ammonia inlet switch valve 10 is closed; the first adsorber high-purity ammonia outlet switch valve 11 is opened; the second adsorber high-purity ammonia outlet switch valve 12 is closed; the first adsorber regeneration nitrogen inlet switch valve 13 is closed; the second adsorber regeneration nitrogen inlet switch valve 14 is opened; the first adsorber regeneration nitrogen outlet switch valve 15 is closed; the second adsorber regeneration nitrogen outlet switch valve 16 is opened; the regeneration nitrogen discharge valve 17 is opened; the pressure reducing device inlet switch valve 18 is closed; the pressure equalizing valve 19 is closed; the heater inlet temperature control valve 20 and the heater outlet temperature control valve 21 are automatically put into operation;

[0063] S5: After purging, a decompression process is performed to discharge the high-purity ammonia in the system; the first adsorber 1 is in the adsorption stage, and the second adsorber 2 is in the decompression stage;

[0064] The valve control status is as follows: close the regeneration nitrogen switch valve 6; the high-purity ammonia backflush valve 7 of the first adsorber is closed, and the high-purity ammonia backflush valve 8 of the first adsorber is closed after the purge is completed; the first adsorber aqueous ammonia inlet switch valve 9 is opened; the second adsorber aqueous ammonia inlet switch valve 10 is closed; the first adsorber high-purity ammonia outlet switch valve 11 is opened; the second adsorber high-purity ammonia outlet switch valve 12 is closed; the first adsorber regeneration nitrogen inlet switch valve 13 is closed; the second adsorber regeneration nitrogen inlet switch valve 14 is opened; the first adsorber regeneration nitrogen outlet switch valve 15 is closed; the second adsorber regeneration nitrogen outlet switch valve 16 is opened; the regeneration nitrogen discharge valve 17 is opened; the pressure reducing device inlet switch valve 18 is opened; the pressure equalizing valve 19 is closed; the heater inlet temperature control valve 20 and the heater outlet temperature control valve 21 are automatically put into operation; the pressure in the second adsorber 2 drops to a vacuum state.

[0065] S6: charging process, using high-purity ammonia to charge the adsorber, and regeneration ends; the first adsorber 1 is in the adsorption stage, and the second adsorber 2 is in the charging stage;

[0066] The valve control status is as follows: close the regeneration nitrogen switch valve 6; the first adsorber high-purity ammonia backflush valve 7 is closed, and the first adsorber high-purity ammonia backflush valve 8 is closed; the first adsorber water-containing ammonia inlet switch valve 9 is opened; the second adsorber water-containing ammonia inlet switch valve 10 is closed; the first adsorber high-purity ammonia outlet switch valve 11 is opened; the second adsorber high-purity ammonia outlet switch valve 12 is closed; the first adsorber regeneration nitrogen inlet switch valve 13 is closed; the second adsorber regeneration nitrogen inlet switch valve 14 is closed; the first adsorber regeneration nitrogen outlet switch valve 15 is closed; the second adsorber regeneration nitrogen outlet switch valve 16 is opened; the regeneration nitrogen discharge valve 17 is opened; the pressure reducing device inlet switch valve 18 is closed; the pressure equalizing valve 19 is opened; the heater inlet temperature control valve 20 and the heater outlet temperature control valve 21 are automatically put into operation;

[0067] S7: After the pressures of the first adsorber 1 and the second adsorber 2 are equalized, the pressure equalizing valve 19 is closed;

[0068] The valve control status is as follows: close the regeneration nitrogen switch valve 6; close the first adsorber high-purity ammonia backflush valve 7, close the first adsorber high-purity ammonia backflush valve 8; open the first adsorber water-containing ammonia inlet switch valve 9; close the second adsorber water-containing ammonia inlet switch valve 10; open the first adsorber high-purity ammonia outlet switch valve 11; close the second adsorber high-purity ammonia outlet switch valve 12; close the first adsorber regeneration nitrogen inlet switch valve 13; close the second adsorber regeneration nitrogen inlet switch valve 14; close the first adsorber regeneration nitrogen outlet switch valve 15; open the second adsorber regeneration nitrogen outlet switch valve 16; open the regeneration nitrogen discharge valve 17; close the pressure reducing device inlet switch valve 18; close the equalizing valve 19; the heater inlet temperature control valve 20 and the heater outlet temperature control valve 21 are automatically put into operation. At this time, the first adsorber 1 is in the adsorption stage, and the second adsorber 2 is on standby.

[0069] In summary, the production process of the present invention combines the intermediate gas hot regeneration gas and the product gas replacement, and the pressure swing regeneration and temperature swing regeneration processes; that is, hot nitrogen is used to regenerate the dehydration adsorbent, and high-purity ammonia is used to purge the adsorber after thermal regeneration, and after purge, the impurity gas is treated by vacuuming to achieve near-zero treatment. The pressure swing regeneration process is provided with a vacuuming process to reduce the content of impurity gases in the system.

[0070] Any numerical value mentioned in the present invention, if there is only an interval of two units between any minimum value and any maximum value, includes all values ​​from the minimum value to the maximum value each time increasing by one unit. For example, if the amount of a component, or the value of a process variable such as temperature, pressure, time, etc. is declared to be 50-90, in this specification it means that 51-89, 52-88... and 69-71 and 70-71 are specifically listed. For non-integer values, 0.1, 0.01, 0.001 or 0.0001 can be appropriately considered as a unit. These are just some specially specified examples. In this application, in a similar manner, all possible combinations of numerical values ​​between the listed minimum and maximum values ​​are considered to have been disclosed.

[0071] It should be noted that the embodiments described above are only used to explain the present invention and do not constitute any limitation to the present invention. The present invention has been described with reference to typical embodiments, but it should be understood that the words used therein are descriptive and explanatory words, rather than restrictive words. The present invention may be modified as specified within the scope of the claims of the present invention, and the present invention may be revised without departing from the scope and spirit of the present invention. Although the present invention described therein relates to specific methods, materials and embodiments, it does not mean that the present invention is limited to the specific examples disclosed therein, on the contrary, the present invention can be extended to all other methods and applications with the same functions.

Claims

1. An adsorption regeneration production process, characterized in that: The production process includes an adsorption process, a decompression process, a thermal regeneration process, a product gas purge process, and a pressurization process.

2. The production process according to claim 1, characterized in that: In the adsorption process, the water-containing raw gas enters the adsorber, the water is removed, and a high-purity product gas is obtained; the water-containing raw gas includes water-containing ammonia; In the decompression process, the adsorbent is partially regenerated by decompression to prepare for the thermal regeneration process; In the thermal regeneration process, the regeneration gas is heated and enters the adsorber to fully regenerate with the adsorbent; the regeneration gas includes nitrogen; The product gas purge process replaces the hot regenerated gas in the adsorber with product gas; the product gas includes high-purity ammonia; The decompression process discharges the product gas in the system; In the pressurization process, the adsorber is pressurized with the product gas, and the regeneration is completed.

3. An adsorption regeneration production system, characterized in that: The system includes a heater, a buffer tank, an adsorber, and a pressure reducing device; the heater is used to heat the regeneration gas; The buffer tank is used to store product gas; The adsorber is used to absorb moisture in the water-containing raw gas; Pressure reducing equipment is used to discharge product gas.

4. The production system according to claim 3, characterized in that: The inlet and outlet of the heater are provided with temperature control valves.

5. The production system according to any one of claims 3 or 4, characterized in that: The adsorber includes a first adsorber and a second adsorber.

6. The production system according to any one of claims 3 to 5, characterized in that: The adsorber is connected to a water-containing raw gas pipeline, and a switch valve is arranged on the pipeline.

7. The production system according to any one of claims 3 to 6, characterized in that: The adsorber is connected to the buffer tank pipeline via a product gas pipeline, and both the inlet and outlet are provided with switch valves.

8. The production system according to any one of claims 3 to 7, characterized in that: The adsorber is connected to a regeneration gas pipeline, and both the inlet and outlet are provided with switch valves.

9. The production system according to any one of claims 3 to 8, characterized in that: The adsorber is connected to the pressure reducing device via a regeneration gas pipeline, a switch valve is provided on the pressure reducing device pipeline, and a regeneration gas outlet switch valve is also provided on the regeneration gas pipeline; and a pressure equalizing valve is provided on the product gas pipeline.

10. Use of the production process according to claim 1 or 2 or the production system according to any one of claims 3 to 9 in the field of producing high-purity ammonia.

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