CN212532296U - Hydrogen extraction device for synthetic ammonia tail gas - Google Patents
Hydrogen extraction device for synthetic ammonia tail gas Download PDFInfo
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- CN212532296U CN212532296U CN202021024209.9U CN202021024209U CN212532296U CN 212532296 U CN212532296 U CN 212532296U CN 202021024209 U CN202021024209 U CN 202021024209U CN 212532296 U CN212532296 U CN 212532296U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The utility model relates to the field of synthetic ammonia tail gas treatment equipment, in particular to a synthetic ammonia tail gas hydrogen-stripping device. The system comprises at least one group of hydrogen extraction system, wherein the hydrogen extraction system comprises an ammonia washing tower, a gas-liquid separator, a desalting water pipeline, a gas outlet, a tube pass inlet, a tube pass outlet and at least two front membrane separators, wherein the lower part of the ammonia washing tower is connected with a purge gas pipeline, the gas-liquid separator is connected to the upper part of the ammonia washing tower through a pipeline, the top of the ammonia washing tower is connected with the desalting water pipeline, the gas outlet at the top of the gas-liquid separator is connected to the tube pass inlet of a steam heater through a pipeline, the tube pass outlet of the steam heater is connected to the raw gas inlets of the at least two front membrane separators in. The utility model can further recover the hydrogen in the tail gas of the synthetic ammonia system, reduce the hydrogen waste, save energy, reduce cost and improve efficiency; the environment-friendly effect is good, no waste water and waste gas are generated, no solid waste is discharged, and good social and environmental benefits are achieved.
Description
Technical Field
The utility model relates to the field of synthetic ammonia tail gas treatment equipment, in particular to a synthetic ammonia tail gas hydrogen-stripping device.
Background
Hydrogen is a main raw material in the production process of synthetic ammonia and is effective gas for synthesizing ammonia. The method improves the utilization rate of hydrogen in the production process of synthetic ammonia, and is the most effective and convenient way for reducing the production cost.
The hydrogen in the existing synthetic ammonia purge gas is recycled by adopting a single-group membrane separation device, the average content of hydrogen in tail gas is 22vol%, and the hydrogen enters a fuel gas pipe network after pressure reduction for a blowing gas boiler and a three-waste mixed combustion furnace to further recycle heat. However, the heat value of the fuel gas is higher, and the nitrous oxide in the outlet flue gas exceeds the standard occasionally due to the fact that the bed layer temperature of the three waste furnaces is high after the fuel gas enters the three waste furnaces for combustion, so that the fuel gas is not well utilized, and partial emptying phenomenon exists.
SUMMERY OF THE UTILITY MODEL
The utility model provides a hydrogen extraction device for synthetic ammonia tail gas, which aims to further recycle hydrogen in the hydrogen recovery tail gas.
The utility model discloses a realize through following technical scheme: a hydrogen extraction device for tail gas of synthetic ammonia comprises at least one group of hydrogen extraction systems,
the hydrogen extraction system comprises an ammonia washing tower, the lower part of which is connected with a purge gas pipeline, a gas-liquid separator, the gas-liquid separator is connected to the upper part of the ammonia washing tower through a pipeline,
the top of the ammonia washing tower is connected with a desalted water pipeline, a gas outlet at the top of the gas-liquid separator is connected with a tube side inlet of the steam heater through a pipeline, a tube side outlet of the steam heater is connected with raw gas inlets of at least two preposed membrane separators in parallel through a pipeline, and non-permeable gas outlets of all the preposed membrane separators are connected with at least one postpositioned membrane separator which is connected together in series through a pipeline.
As a further improvement of the technical proposal of the utility model, the non-permeable gas outlet of the post-membrane separator at the tail end is connected in parallel to at least two tail-membrane separators through pipelines.
As the technical scheme of the utility model further improve, wash the aqueous ammonia export of ammonia tower bottom and the aqueous ammonia export of vapour and liquid separator bottom and put together and through the line connection to the aqueous ammonia system of urea through the pipeline.
As a further improvement of the technical proposal of the utility model, the hydrogen extracting system is divided into two groups.
Compared with the prior art, the hydrogen extraction device for the synthetic ammonia tail gas can further recover the hydrogen in the tail gas of the synthetic ammonia system, reduce the hydrogen waste, save energy, reduce cost and improve efficiency; the method has the advantages of good environment-friendly effect, further reduction of the tail gas emission of the synthetic ammonia, no waste water, no waste gas and no solid waste emission under normal operation conditions, good social and environmental benefits, relatively simple operation and higher safety.
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 description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only 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 stripping device for tail gas of synthetic ammonia provided by an embodiment.
In the figure: 1-purge gas discharge pipeline, 2-ammonia washing tower, 3-desalination water pipeline, 4-gas-liquid separator, 5-steam heater, 6-preposed membrane separator, 7-postpositional membrane separator and 8-tailed membrane separator.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention clearer, the technical solutions of the present invention will be described in detail below. It is to be understood that the embodiments described are only some embodiments of the invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.
As shown in FIG. 1, the present embodiment provides a hydrogen extraction device for tail gas of ammonia synthesis, which comprises two hydrogen extraction systems, wherein each hydrogen extraction system comprises an ammonia scrubber 2 connected with a purge gas line 1 at the lower part, a gas-liquid separator 4 connected to the upper part of the ammonia scrubber 2 through a pipeline,
the top of the ammonia washing tower 2 in each group of hydrogen extraction systems is connected to a desalting water pipeline 3, the gas outlet at the top of the gas-liquid separator 4 is connected to the tube side inlet of a steam heater 5 through a pipeline, the tube side outlet of the steam heater 5 is connected to the raw gas inlet of two preposed membrane separators 6 in parallel through a pipeline, the non-permeable gas outlets of all the preposed membrane separators 6 of the first group of hydrogen extraction systems are connected to two postpositional membrane separators 7 connected in series through a pipeline (see the lower part of the figure 1), and the non-permeable gas outlets of all the preposed membrane separators 6 of the second group of hydrogen extraction systems are connected to one postpositional membrane separator 7 through a pipeline (see the upper part of the figure 1).
In this embodiment, the purge gas (synthesis ammonia tail gas) in the purge gas line 1 mainly comprises ammonia, methane, nitrogen, hydrogen and argon, and the flow of the purge gas in the two sets of hydrogen extraction systems is adjusted by valves according to the requirement of the hydrogen content in the required non-permeate gas in the fuel gas pipe network, the purge gas firstly enters the ammonia washing tower 2 (i.e. the water washing tower) in the two sets of hydrogen extraction systems to be in contact washing with the desalted water from the top of the ammonia washing tower 2, so that the ammonia concentration in the gas discharged from the tower is less than 10ppm, and the higher ammonia concentration is harmful to the membrane separator. And in addition, two high-pressure water pumps are arranged in each group of hydrogen extraction systems to convey desalted water from a desalting water pipeline 3 to the top of an ammonia washing tower 2, ammonia in raw material gas is washed, and one water pump works and the other water pump works for standby. Preferably, the ammonia scrubber 2 is equipped with wire mesh packing so that the gas and liquid can be sufficiently contacted. After the purge gas comes out of the upper part of the ammonia scrubber 2, the temperature is about 25 ℃, and then the purge gas is introduced into the gas-liquid separator 4, and then the gas-liquid separator 4 removes the mist. Then into a steam heater 5, which heats the purge gas high to its dew point to 50 ℃. If the purge gas (raw gas) after washing is not heated to a high dew point, the liquid will condense on the fiber surface of the membrane separator, resulting in a decrease in recovery. In this embodiment, the steam heater 5 is a double-pipe heat exchanger, the raw gas is in the pipe, and the steam is on the shell side, wherein the steam comes from the pipe network of the synthetic ammonia production system. In order to ensure that the steam heater 5 is properly heated, the steam heater 5 is provided with a raw material gas temperature alarm and an outlet temperature high-temperature linkage.
The raw gas of the first group of hydrogen extraction system is heated by a steam heater 5 and then respectively enters two preposed membrane separators 6, the non-permeable gas of the two preposed membrane separators 6 is connected to two postpositional membrane separators 7 which are connected together in series through a pipeline, the non-permeable gas outlet between the first postpositional membrane separator 7 is connected to the raw gas inlet of the second postpositional membrane separator 7, after the purge gas passes through the two preposed membrane separators 6 and the two postpositional membrane separators 7, the permeable gas of each membrane separator is returned to the synthetic ammonia production system together, at the moment, the hydrogen content in the permeable gas is more than 93 percent, and the hydrogen content in the non-permeable gas returned to the production system is about 19 percent.
The raw gas of the second group of hydrogen extraction system is heated by a steam heater 5 and then respectively enters two preposed membrane separators 6, the non-permeable gas of the two preposed membrane separators 6 is connected to a postpositive membrane separator 7 through a pipeline, when the purge gas passes through the two preposed membrane separators 6 and the postpositive membrane separator 7, the permeable gas of each membrane separator returns to the synthetic ammonia production system together, at the moment, the content of hydrogen in the permeable gas returning to the production system is more than 91 percent, and the content of hydrogen in the non-permeable gas is about 24 percent.
In the embodiment, because the gas amount of the purge gas is large, the feed gas is heated by the steam heater 5 and then respectively enters the two pre-membrane separators 6, so that the flow dividing effect can be achieved, the gas amount of the non-permeable gas respectively entering the two pre-membrane separators 6 for separation is greatly reduced, and the service life of the post-membrane separator 7 can be prolonged.
In the embodiment, in order to further recycle the hydrogen in the non-permeate gas, the non-permeate gas outlets of the post-membrane separators 7 at the tail ends of the two groups of hydrogen extraction systems are connected in parallel to the three tail-membrane separators 8 through pipelines on the premise of avoiding changing the existing hydrogen extraction system equipment. The non-permeable gas of each tail membrane separator 8 is jointly conveyed to a fuel gas pipe network through a pipeline, the permeable gas is jointly returned to the synthetic ammonia production system, the content of hydrogen in the permeable gas returned to the production system is more than 82%, and the content of hydrogen in the non-permeable gas is about 4.7%.
As shown in figure 1, an ammonia water outlet at the bottom of the ammonia washing tower 2 and an ammonia water outlet at the bottom of the gas-liquid separator 4 are combined together through a pipeline and are connected into an ammonia water system of urea through a pipeline.
The above description is only for the specific embodiments of the present invention, but the protection scope of the present invention is not limited thereto, and any person skilled in the art can easily think of the changes or substitutions within the technical scope of the present invention, and all should be covered within the protection scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (5)
1. A hydrogen extraction device for tail gas of synthetic ammonia is characterized by comprising at least one group of hydrogen extraction systems,
the hydrogen extraction system comprises an ammonia washing tower (2) the lower part of which is connected with a purge gas pipeline (1), a gas-liquid separator (4) which is connected to the upper part of the ammonia washing tower (2) through a pipeline,
the top of the ammonia washing tower (2) is connected to a desalted water pipeline (3), a gas outlet at the top of the gas-liquid separator (4) is connected to a tube side inlet of a steam heater (5) through a pipeline, tube side outlets of the steam heater (5) are connected to feed gas inlets of at least two preposed membrane separators (6) in parallel through pipelines, and non-permeable gas outlets of all the preposed membrane separators (6) are connected to at least one postpositioned membrane separator (7) connected together in series through a pipeline.
2. A hydrogen stripping device for tail gas of synthetic ammonia according to claim 1, characterized in that the non-permeate outlet of the post-membrane separator (7) at the tail end is connected in parallel to at least two tail membrane separators (8) by a pipeline.
3. The device for stripping hydrogen from synthesis ammonia tail gas according to claim 1 or 2, characterized in that the ammonia water outlet at the bottom of the ammonia washing tower (2) and the ammonia water outlet at the bottom of the gas-liquid separator (4) are combined together through a pipeline and connected into an ammonia water system of urea through a pipeline.
4. The device for stripping hydrogen from synthesis ammonia tail gas according to claim 1 or 2, characterized in that the hydrogen stripping systems are two groups.
5. The device for stripping hydrogen from synthesis ammonia tail gas according to claim 3, characterized in that the hydrogen stripping systems are two groups.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021024209.9U CN212532296U (en) | 2020-06-08 | 2020-06-08 | Hydrogen extraction device for synthetic ammonia tail gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021024209.9U CN212532296U (en) | 2020-06-08 | 2020-06-08 | Hydrogen extraction device for synthetic ammonia tail gas |
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| CN212532296U true CN212532296U (en) | 2021-02-12 |
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| CN202021024209.9U Active CN212532296U (en) | 2020-06-08 | 2020-06-08 | Hydrogen extraction device for synthetic ammonia tail gas |
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