CN219098754U - Synthetic ammonia combined hydrogen production system utilizing process gas at outlet of cold box - Google Patents
Synthetic ammonia combined hydrogen production system utilizing process gas at outlet of cold box Download PDFInfo
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- CN219098754U CN219098754U CN202223297342.3U CN202223297342U CN219098754U CN 219098754 U CN219098754 U CN 219098754U CN 202223297342 U CN202223297342 U CN 202223297342U CN 219098754 U CN219098754 U CN 219098754U
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Abstract
The technical scheme includes that the synthesis ammonia combined hydrogen production system comprises a synthesis ammonia system and a hydrogen production system, wherein the synthesis ammonia system comprises a cold box outlet pipeline and a primary reformer, the hydrogen production system comprises a gas-water separator and a pressure swing adsorption device, the pressure swing adsorption device comprises an adsorption tower, the cold box outlet pipeline is provided with a separator inlet pipe, the separator inlet pipe is connected to the gas-water separator, a gas phase outlet of the gas-water separator is connected to the adsorption tower through an adsorption inlet pipe, a hydrogen outlet pipe of the adsorption tower is connected to a hydrogen buffer tank, a desorption gas outlet pipe of the adsorption tower is connected to a desorption gas buffer tank and a desorption gas mixing tank, and the desorption gas mixing tank is connected to the primary reformer through a desorption gas pipe. The utility model adopts the process gas at the outlet of the cold box as the raw material for hydrogen production, has smaller pressure and almost no water, not only can reduce the safety risk of hydrogen production equipment, but also can effectively prolong the service life of the hydrogen production adsorbent.
Description
Technical Field
The utility model relates to the technical field of hydrogen production by synthesis of ammonia, in particular to a combined hydrogen production system by synthesis of ammonia by utilizing process gas at an outlet of a cold box.
Background
One common process for synthesizing ammonia is a cryogenic purification process, and raw materials are synthesized into ammonia products through the working procedures of primary conversion, secondary conversion, conversion and decarbonization, methanation and drying, cold box, compression, synthesis and the like. The cold box is core equipment in the cryogenic purification process, has the key effects of removing inert components, adjusting the synthetic hydrogen-nitrogen ratio and guaranteeing the synthetic efficiency, and the outlet process gas of the cold box is mainly hydrogen and nitrogen after the cryogenic purification of the cold box.
In the existing co-production of hydrogen by synthesizing ammonia, the raw materials used for hydrogen production come from process gas at the outlet of an ammonia recovery system, but the pressure is too high to 3.5 MPa, and the water content is higher, so that the safe operation of hydrogen production equipment is threatened, and the service life of a hydrogen production adsorbent is shortened.
Disclosure of Invention
Aiming at the problems that the service lives of hydrogen production equipment and adsorbent are influenced by the excessive high process air pressure and the large water content of an outlet process air of an ammonia recovery system in the prior art, the utility model provides a combined synthetic ammonia hydrogen production system utilizing the process air of an outlet of a cold box.
The utility model provides the following technical scheme: the utility model provides an utilize synthetic ammonia of cold box export process gas to unite hydrogen manufacturing system, includes synthetic ammonia system and hydrogen manufacturing system, synthetic ammonia system includes cold box export pipeline and one section reformer, hydrogen manufacturing system includes gas-water separator and pressure swing adsorption device, pressure swing adsorption device includes the adsorption tower, cold box export pipeline is provided with the separator import pipe, the separator import pipe is connected to gas-water separator, the gaseous phase export of gas-water separator is connected to the adsorption tower through the absorption import pipe, the hydrogen outlet pipe of adsorption tower is connected to the hydrogen buffer tank, the analytic gas outlet pipe of adsorption tower is connected to analytic gas buffer tank, analytic gas mixing tank is connected to one section reformer through analytic gas pipeline.
Preferably, the separator inlet pipe, the hydrogen outlet pipe and the desorption gas pipeline are provided with pressure regulating valves.
Preferably, the pressure swing adsorption device comprises a plurality of adsorption tower groups arranged in parallel; each adsorption tower group comprises two adsorption towers, adsorption inlet pipes of the two adsorption towers are connected to the adsorption inlet branch pipe, hydrogen outlet pipes of the two adsorption towers are connected to the hydrogen outlet branch pipe, and desorption gas outlet pipes of the two adsorption towers are connected to the desorption gas outlet branch pipe; the adsorption inlet branch pipes of the adsorption tower groups are connected to an adsorption inlet main pipe, the adsorption inlet main pipe is connected with a gas phase outlet of the gas-water separator, the hydrogen outlet branch pipes of the adsorption tower groups are connected to a hydrogen outlet main pipe, the hydrogen outlet main pipe is connected to a hydrogen buffer tank, the desorption gas outlet branch pipes of the adsorption tower groups are connected to a desorption gas outlet main pipe, and the desorption gas outlet main pipe is connected to a desorption gas buffer tank; and the adsorption inlet branch pipe, the hydrogen outlet branch pipe and the analysis gas outlet branch pipe are all provided with stop valves.
Preferably, the purge gas outlet pipe is provided with a direct connection pipe connected to the purge gas mixing tank.
The beneficial effects of the utility model are as follows: the process gas at the outlet of the cold box is used as the hydrogen production raw material, the pressure is small and almost no water is contained, the safety risk of hydrogen production equipment can be reduced, the service life of the hydrogen production adsorbent can be effectively prolonged, the long-period operation of the hydrogen production system is ensured, and the separated resolved gas can be sent to a first-stage reformer of the ammonia synthesis system for reuse.
Drawings
Fig. 1 is a device connection diagram of one embodiment of the present utility model.
FIG. 2 is a schematic diagram showing the connection of equipment in one embodiment of the pressure swing adsorption apparatus of the present utility model.
Reference numerals: 10-cold box outlet pipe, 11-primary reformer, 20-gas-water separator, 21-separator inlet pipe, 30-adsorption tower, 31-adsorption inlet pipe, 311-adsorption inlet branch pipe, 312-adsorption inlet header pipe, 32-hydrogen outlet pipe, 321-hydrogen outlet branch pipe, 322-hydrogen outlet header pipe, 33-desorption gas outlet pipe, 331-desorption gas outlet branch pipe, 332-desorption gas outlet header pipe, 34-direct connection pipe, 40-hydrogen buffer tank, 50-desorption gas buffer tank, 60-desorption gas mixing tank, 61-desorption gas pipe, and 70-pressure regulating valve.
Detailed Description
Embodiments of the present utility model will be described in more detail below with reference to the drawings and reference numerals, so that those skilled in the art can practice the present utility model after studying the specification. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the utility model.
Example 1
The utility model provides a combined synthetic ammonia hydrogen production system utilizing cold box outlet process gas, as shown in fig. 1, which comprises a synthetic ammonia system and a hydrogen production system, wherein the synthetic ammonia system comprises a cold box outlet pipeline 10 and a primary reformer 11, the hydrogen production system comprises a gas-water separator 20 and a pressure swing adsorption device, and the pressure swing adsorption device comprises an adsorption tower 30. In the synthetic ammonia system, generally comprises a first-stage conversion section, a second-stage conversion section, a decarbonization section, a methanation section, a drying section, a cold box section, a compression section, a synthesis section and the like, wherein a cold box outlet pipeline 10 is used for connecting the cold box section and the compression section, the cold box outlet process gas mainly comprises hydrogen and nitrogen, almost contains no water, the pressure is only about 2.35 MPa, and compared with the gas pressure of the outlet process gas of an ammonia recovery system adopted in the prior art, the pressure is smaller, so that the safety of hydrogen production equipment can be effectively ensured.
Therefore, the utility model adopts the process gas at the outlet of the cold box to produce hydrogen. Specifically, the cold box outlet pipe 10 is provided with a separator inlet pipe 21, the separator inlet pipe 21 is connected to the gas-water separator 20, a gas phase outlet of the gas-water separator 20 is connected to the adsorption tower 30 through an adsorption inlet pipe 31, a hydrogen outlet pipe 32 of the adsorption tower 30 is connected to a hydrogen buffer tank 40, a desorption gas outlet pipe 33 of the adsorption tower 30 is connected to a desorption gas buffer tank 50, a desorption gas mixing tank 60, and the desorption gas mixing tank 60 is connected to the primary reformer 11 through a desorption gas pipe 61.
The separator inlet pipe 21 serves as a branch pipe of the cold box outlet pipe 10, and branches a part of the cold box outlet process gas to the hydrogen production system, and the other part is left in the ammonia synthesis system, and the separator inlet pipe 21 is provided with a stop valve. The gas-water separator 20 separates free water in the process gas at the outlet of the cold box and then sends the gas into an adsorption tower through an adsorption inlet pipe 31; the adsorption tower 30 separates the hydrogen from the process gas at the outlet of the cold box into hydrogen and desorption gas by using a pressure swing adsorption process, wherein the composition of the desorption gas mainly comprises hydrogen, nitrogen and argon; hydrogen enters a hydrogen buffer tank 40 from the top of the adsorption tower through a hydrogen outlet pipe 32 and then is sent out of the boundary region, and the analysis gas sequentially enters an analysis gas buffer tank 50 and an analysis gas mixing tank through an analysis gas outlet pipe 33 for buffering and mixing and then is sent into a primary reformer of the ammonia synthesis system to be used as fuel.
Further, the separator inlet pipe 21, the hydrogen outlet pipe 42, and the desorption gas pipe 61 are provided with pressure regulating valves 70, so that the gas pressure entering the gas-water separator, the hydrogen buffer tank, and the primary reformer is more stable, respectively.
Further, the purge gas outlet pipe 33 is provided with a direct connection pipe 34, and the direct connection pipe 34 is connected to the purge gas mixing tank 60.
Example 2
The utility model provides a combined hydrogen production system for synthesis ammonia by utilizing process gas at an outlet of a cold box, which is characterized in that on the basis of an embodiment 1, a pressure swing adsorption device comprises a plurality of adsorption tower groups which are arranged in parallel, and because a certain time is required for adsorbent regeneration, the plurality of adsorption tower groups are arranged in parallel to realize continuous production by circulating work.
Specifically, as shown in fig. 2, there are 3 adsorption tower groups in total, each adsorption tower group includes two adsorption towers 30, adsorption inlet pipes 31 of the two adsorption towers 30 are connected to an adsorption inlet branch pipe 311, hydrogen outlet pipes 32 of the two adsorption towers are connected to a hydrogen outlet branch pipe 321, and desorption gas outlet pipes 33 of the two adsorption towers are connected to a desorption gas outlet branch pipe 331; the adsorption inlet branch pipes 311 of the plurality of adsorption tower groups are all connected to an adsorption inlet main pipe 312, the adsorption inlet main pipe 312 is connected with the gas phase outlet of the gas-water separator 20, the hydrogen outlet branch pipes 321 of the plurality of adsorption tower groups are all connected to a hydrogen outlet main pipe 322, the hydrogen outlet main pipe 322 is connected to a hydrogen buffer tank 40, the desorption gas outlet branch pipes 331 of the plurality of adsorption tower groups are all connected to a desorption gas outlet main pipe 332, and the desorption gas outlet main pipe 332 is connected to a desorption gas buffer tank 50; the adsorption inlet branch pipe 311, the hydrogen outlet branch pipe 321 and the desorption gas outlet branch pipe 331 are all provided with stop valves. When one adsorption tower group works, the stop valves of other adsorption tower groups are closed, and a plurality of adsorption tower groups work circularly, so that continuous production is realized.
The foregoing is a description of one or more embodiments of the utility model, which are specific and detailed, but are not to be construed as limiting the scope of the utility model. It should be noted that it will be apparent to those skilled in the art that several variations and modifications can be made without departing from the spirit of the utility model, which are all within the scope of the utility model. Accordingly, the scope of protection of the present utility model is to be determined by the appended claims.
Claims (4)
1. The utility model provides an utilize synthetic ammonia of cold box export process gas to unite hydrogen manufacturing system, includes synthetic ammonia system and hydrogen manufacturing system, synthetic ammonia system includes cold box export pipeline (10) and one section converter (11), hydrogen manufacturing system includes gas-water separator (20) and pressure swing adsorption device, pressure swing adsorption device includes adsorption tower (30), its characterized in that: the cold box outlet pipeline (10) is provided with a separator inlet pipe (21), the separator inlet pipe (21) is connected to the gas-water separator (20), a gas phase outlet of the gas-water separator (20) is connected to the adsorption tower (30) through an adsorption inlet pipe (31), a hydrogen outlet pipe (32) of the adsorption tower (30) is connected to the hydrogen buffer tank (40), a resolved gas outlet pipe (33) of the adsorption tower (30) is connected to the resolved gas buffer tank (50) and the resolved gas mixing tank (60), and the resolved gas mixing tank (60) is connected to the primary reformer (11) through a resolved gas pipeline (61).
2. A combined ammonia production system utilizing cold box outlet process gas as defined in claim 1, wherein: the separator inlet pipe (21), the hydrogen outlet pipe (32) and the analysis gas pipe (61) are provided with pressure regulating valves (70).
3. A combined ammonia production system utilizing cold box outlet process gas as defined in claim 1, wherein: the pressure swing adsorption device comprises a plurality of adsorption tower groups which are arranged in parallel;
each adsorption tower group comprises two adsorption towers (30), an adsorption inlet pipe (31) of each adsorption tower (30) is connected to an adsorption inlet branch pipe (311), a hydrogen outlet pipe (32) of each adsorption tower is connected to a hydrogen outlet branch pipe (321), and a desorption gas outlet pipe (33) of each adsorption tower is connected to a desorption gas outlet branch pipe (331);
the adsorption inlet branch pipes (311) of the adsorption tower groups are all connected to an adsorption inlet main pipe (312), the adsorption inlet main pipe (312) is connected with a gas phase outlet of the gas-water separator (20), the hydrogen outlet branch pipes (321) of the adsorption tower groups are all connected to a hydrogen outlet main pipe (322), the hydrogen outlet main pipe (322) is connected to a hydrogen buffer tank (40), the desorption gas outlet branch pipes (331) of the adsorption tower groups are all connected to a desorption gas outlet main pipe (332), and the desorption gas outlet main pipe (332) is connected to a desorption gas buffer tank (50);
the adsorption inlet branch pipe (311), the hydrogen outlet branch pipe (321) and the desorption gas outlet branch pipe (331) are respectively provided with a stop valve.
4. A combined ammonia production system utilizing cold box outlet process gas as defined in claim 1, wherein: the purge gas outlet pipe (33) is provided with a direct connection pipe (34), and the direct connection pipe (34) is connected to a purge gas mixing tank (60).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202223297342.3U CN219098754U (en) | 2022-12-09 | 2022-12-09 | Synthetic ammonia combined hydrogen production system utilizing process gas at outlet of cold box |
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| CN202223297342.3U CN219098754U (en) | 2022-12-09 | 2022-12-09 | Synthetic ammonia combined hydrogen production system utilizing process gas at outlet of cold box |
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| CN219098754U true CN219098754U (en) | 2023-05-30 |
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