CN217838400U - Hydrogen recycling system of ammonia synthesis device - Google Patents
Hydrogen recycling system of ammonia synthesis device Download PDFInfo
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- CN217838400U CN217838400U CN202222176223.6U CN202222176223U CN217838400U CN 217838400 U CN217838400 U CN 217838400U CN 202222176223 U CN202222176223 U CN 202222176223U CN 217838400 U CN217838400 U CN 217838400U
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Abstract
The utility model relates to a non-permeate gas utilization field is retrieved to synthetic ammonia device's hydrogen specifically is a synthetic ammonia device hydrogen recycle system, set up the one-level membrane separator in the speed gassing intake pipe including at least one side by side, set up the second grade membrane separator in the non-permeate gas export of all one-level membrane separators, connect the hydrogen recovery pipe in the permeate gas export of all membrane separators, still include cryogenic heat exchanger, methane rectifying column and liquid argon rectifying column. The non-permeate gas is deeply cooled and rectified, the outlet gas returns to a synthetic ammonia system to be used as a raw material gas, and the liquefied methane and the liquid argon which are deeply cooled and separated are respectively recovered, so that the liquefied methane has a wide market, can be used as civil gas and automobile gas, and can be used as effective supplement of natural gas; the liquid argon can serve the electronic industry market of high-purity gas, bring new benefit growth to companies and increase the strategic development space of the companies.
Description
Technical Field
The utility model relates to the field of the utilization of non-permeable gas for the hydrogen recovery of a synthetic ammonia device, in particular to a hydrogen recovery system of a synthetic ammonia device.
Background
The main method for recovering hydrogen at present in the hydrogen recovery section of an ammonia synthesis device is a semi-permeable membrane method, permeated gas hydrogen is recovered to the ammonia synthesis device for recycling, non-permeated gas is depressurized by a pressure reducing valve and then is sent to a boiler for combustion, and lump carbon which can be used as a fertilizer production raw material is subjected to a series of complex processes to generate steam.
SUMMERY OF THE UTILITY MODEL
The utility model provides a hydrogen recycling system of a synthetic ammonia device, which solves the problem of unreasonable energy utilization of a hydrogen recycling workshop section.
The utility model discloses a realize through following technical scheme: the hydrogen recycling system of the ammonia synthesis device comprises at least one primary membrane separator arranged on a purge gas inlet pipe side by side, secondary membrane separators arranged on non-permeation gas outlets of all the primary membrane separators, hydrogen recovery pipes connected to permeation gas outlets of all the membrane separators, a cryogenic heat exchanger, a methane rectifying tower and a liquid argon rectifying tower,
the inside passageway A, passageway B and the passageway C that has of cryrogenic heat exchanger, the non-permeate gas exit linkage of second grade membrane separator is in the passageway A entrance point of cryrogenic heat exchanger, passageway A exit end links to each other with the feed inlet of methane rectifying column, the bottom liquid outlet of methane rectifying column passes through pipe connection to liquid methane LNG storage tank, the top export of methane rectifying column links to each other with the passageway B entrance point of cryrogenic heat exchanger, passageway B exit end links to each other with the feed inlet of liquid argon rectifying column, the bottom liquid outlet of liquid argon rectifying column passes through pipe connection to liquid argon storage tank, the top export of liquid argon rectifying column links to each other with the passageway C entrance point of cryrogenic heat exchanger, passageway C exit end is connected with hydrogen nitrogen gas recovery pipe.
As the further improvement of the technical proposal of the utility model, the cold quantity of the cryogenic heat exchanger is provided by the refrigerating unit.
As the technical scheme of the utility model is further improved, connect in parallel on the non-permeate gas export of second grade membrane separator has non-permeate gas recovery tube, it is provided with the fourth valve to establish ties on the non-permeate gas recovery tube, it is provided with the fifth valve to establish ties on the pipeline between non-permeate gas recovery tube and cryogenic heat exchanger's the passageway A entrance point.
As a further improvement of the technical proposal of the utility model, the number of the primary membrane separators is two.
Compared with the prior art, the hydrogen recycling system of the ammonia synthesis device has the following beneficial effects:
the non-permeate gas is deeply cooled and rectified, the outlet gas returns to a synthetic ammonia system to be used as a raw material gas, and the liquefied methane and the liquid argon which are deeply cooled and separated are respectively recovered, so that the liquefied methane has a wide market, can be used as civil gas and automobile gas, and can be used as effective supplement of natural gas; the liquid argon can serve the electronic industry market of high-purity gas, bring new benefit growth to companies and increase the strategic development space of the companies.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments or the technical solutions in the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a schematic structural diagram of a hydrogen recycling system of an ammonia synthesis device of the present invention.
FIG. 2 is a schematic connection diagram of the cryogenic heat exchanger, the methane rectifying column and the liquid argon rectifying column.
In the figure: 1-purge gas inlet pipe, 2-primary membrane separator, 3-secondary membrane separator, 4-cryogenic heat exchanger, 5-methane rectifying tower, 6-liquid argon rectifying tower, 7-hydrogen nitrogen recovery pipe, 8-refrigerating unit, 9-hydrogen recovery pipe, 10-non-permeate gas recovery pipe, 14-fourth valve and 15-fifth valve.
Detailed Description
The technical solutions of the present invention will be described clearly and completely below, and it should be apparent that the described embodiments are some, but not all embodiments of the present invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "first" and "second" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
As shown in figures 1 and 2, the utility model provides a specific embodiment of a hydrogen recycling system of an ammonia synthesis device, which comprises two primary membrane separators 2 which are arranged on a purge gas inlet pipe 1 side by side, secondary membrane separators 3 which are arranged on non-permeate gas outlets of all the primary membrane separators 2, hydrogen recycling pipes 9 which are connected on permeate gas outlets of all the membrane separators, a cryogenic heat exchanger 4, a methane rectifying tower 5 and a liquid argon rectifying tower 6,
4 inside passageway A, passageway B and the passageway C of having of cryrogenic heat exchanger, the non-permeate gas exit linkage of second grade membrane separator 3 is in the passageway A entrance point of cryrogenic heat exchanger 4, passageway A exit end links to each other with the feed inlet of methane rectifying column 5, the bottom liquid outlet of methane rectifying column 5 passes through pipeline connection to liquid methane LNG storage tank, the top export of methane rectifying column 5 links to each other with the passageway B entrance point of cryrogenic heat exchanger 4, passageway B exit end links to each other with the feed inlet of liquid argon rectifying column 6, the bottom liquid outlet of liquid argon rectifying column 6 passes through pipeline connection to liquid argon storage tank, the top export of liquid argon rectifying column 6 links to each other with the passageway C entrance point of cryrogenic heat exchanger 4, passageway C exit end is connected with hydrogen nitrogen gas recovery pipe 7.
The critical temperature of methane is-82.57 ℃, the critical temperature of argon is-122.29 ℃, the critical temperature of hydrogen is-252 ℃, the critical temperature of nitrogen is-195 ℃, and the separation and purification of gas are realized by utilizing the principle that the liquefaction temperatures of all components of non-permeable gas are different. The purge gas from the synthesis post is in countercurrent contact with soft water sprayed from the top of the tower in a water washing tower, ammonia in the purge gas is absorbed, the ammonia is discharged from the top of the tower, moisture is separated by a separator, the purge gas is heated by a heater and then enters a primary membrane separator 2 through a purge gas inlet pipe 1, non-permeable gas separated from the primary membrane separator 2 enters a secondary membrane separator 3, permeable gas hydrogen of the primary membrane separator 2 and the secondary membrane separator 3 are gathered together and recycled through a hydrogen recycling pipe 9, non-permeable gas separated by the secondary membrane separator 3 enters a channel A of a cryogenic heat exchanger 4, the non-permeable gas in the channel A is cooled to below-82.57 ℃, liquid methane is conveyed to a liquid methane LNG (liquefied natural gas) through a bottom liquid outlet after entering a methane rectification tower 5, the gas-liquid mixture enters a channel B through a top outlet of the methane rectification tower 5 and is further cooled to below-122.29 ℃, the gas-liquid mixture enters a liquid rectification tower 6, the liquid is conveyed to the liquid methane LNG storage tank through a bottom liquid outlet, the low-temperature-gas-liquid-gas mixture enters a hydrogen outlet of the argon rectification tower 6 and enters a hydrogen-gas channel C of the argon rectification tower, the hydrogen-gas-nitrogen-ammonia synthesis system, and the nitrogen mixture are heated by a nitrogen recycling system, and the nitrogen-ammonia synthesis system.
The liquefied methane has wide market, can be used as civil gas and automobile gas filling, and can be used as effective supplement of natural gas; the high-purity argon can serve the electronic industry market of high-purity gas, bring new benefit growth to companies, and simultaneously can increase strategic development space of the companies. Analyzed by economic benefit according to 10000Nm 3 Per hour venting gas to account for H 2 =63% N 2 =22%, methane =9%, ammonia =2%, argon = 2.5%) hourly recovery of methane 900Nm 3 250Nm of argon gas recovered 3 According to the market price of methane, 2.7 yuan/m 3 And the market price of argon is 15 yuan/m 3 And the annual running time is 7200 hours, the hourly output value is 6180 yuan, the annual output value is 4450 ten thousand yuan, and the benefit is good.
As shown in fig. 2, the cooling capacity of the cryogenic heat exchanger 4 is provided by a refrigeration unit 8.
As shown in FIG. 1, the non-permeate gas outlet of the secondary membrane separator 3 is connected with a non-permeate gas recovery pipe 10 in parallel, a fourth valve 14 is connected in series on the non-permeate gas recovery pipe 10, and a fifth valve 15 is connected in series on a pipeline between the non-permeate gas recovery pipe 10 and the inlet end of the channel A of the cryogenic heat exchanger 4. When parts such as the cryogenic heat exchanger 4, the methane rectifying tower 5 and the liquid argon rectifying tower 6 need to be overhauled, the fifth valve 15 is closed, the fourth valve 14 is opened, and the non-permeable gas in the non-permeable gas recovery pipe 10 is sent to the boiler for combustion after being reduced in pressure by the pressure reducing valve. After the parts such as the cryogenic heat exchanger 4, the methane rectifying tower 5, the liquid argon rectifying tower 6 and the like are overhauled, the fourth valve 14 is closed, the fifth valve 15 is opened, and cryogenic cooling and rectification of the non-permeable gas are continuously completed.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; although the present invention has been described in detail with reference to the foregoing embodiments, it should be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; such modifications and substitutions do not depart from the spirit and scope of the present invention.
Claims (4)
1. The hydrogen recycling system of the ammonia synthesis device comprises at least one primary membrane separator (2) which is arranged on a purge gas inlet pipe (1) side by side, secondary membrane separators (3) which are arranged on non-permeation gas outlets of all the primary membrane separators (2), and hydrogen recycling pipes (9) which are connected to permeation gas outlets of all the membrane separators, and is characterized by further comprising a cryogenic heat exchanger (4), a methane rectifying tower (5) and a liquid argon rectifying tower (6),
the inside passageway A, passageway B and passageway C that has of cryrogenic heat exchanger (4), the non-permeate gas exit linkage of second grade membrane separator (3) is in the passageway A entrance point of cryrogenic heat exchanger (4), passageway A exit end links to each other with the feed inlet of methane rectifying column (5), the bottom liquid outlet of methane rectifying column (5) passes through pipe connection to liquid methane LNG storage tank, the top export of methane rectifying column (5) links to each other with the passageway B entrance point of cryrogenic heat exchanger (4), passageway B exit end links to each other with the feed inlet of liquid argon rectifying column (6), the bottom liquid outlet of liquid argon rectifying column (6) passes through pipe connection to liquid argon storage tank, the top export of liquid argon rectifying column (6) links to each other with the passageway C entrance point of cryrogenic heat exchanger (4), passageway C exit end is connected with hydrogen gas recovery pipe (7).
2. The ammonia plant hydrogen recycling system according to claim 1, characterized in that the refrigeration capacity of the cryogenic heat exchanger (4) is provided by a refrigeration unit (8).
3. The ammonia plant hydrogen recycling system according to claim 1, characterized in that the non-permeate gas outlet of the secondary membrane separator (3) is connected with a non-permeate gas recycling pipe (10) in parallel, the non-permeate gas recycling pipe (10) is provided with a fourth valve (14) in series, and a fifth valve (15) is provided in series on a pipeline between the non-permeate gas recycling pipe (10) and the inlet end of the channel A of the cryogenic heat exchanger (4).
4. A synthesis ammonia plant hydrogen recycling system according to claim 1, characterized in that the number of the primary membrane separators (2) is two.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202222176223.6U CN217838400U (en) | 2022-08-18 | 2022-08-18 | Hydrogen recycling system of ammonia synthesis device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202222176223.6U CN217838400U (en) | 2022-08-18 | 2022-08-18 | Hydrogen recycling system of ammonia synthesis device |
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| CN217838400U true CN217838400U (en) | 2022-11-18 |
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| CN202222176223.6U Active CN217838400U (en) | 2022-08-18 | 2022-08-18 | Hydrogen recycling system of ammonia synthesis device |
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