CN210752112U - Coking ammonia recycle system - Google Patents
Coking ammonia recycle system Download PDFInfo
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- CN210752112U CN210752112U CN201920873621.9U CN201920873621U CN210752112U CN 210752112 U CN210752112 U CN 210752112U CN 201920873621 U CN201920873621 U CN 201920873621U CN 210752112 U CN210752112 U CN 210752112U
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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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The utility model belongs to the technical field of the chemical industry, especially, relate to a coking ammonia recycle system, including the storage tank that is used for depositing the aqueous ammonia, first ceramic filter, tar remover, first heat exchanger, deacidification ammonia still, ammonia dephlegmator, first ammonia condensation cooler, strong aqueous ammonia buffer tank, second ceramic filter, strong aqueous ammonia intermediate tank, second heat exchanger, aqueous ammonia rectifying column, second ammonia condensation cooler and ammonia buffer tank; the utility model discloses the ammonia of the effective recycle surplus aqueous ammonia production of product replaces original design and carries out coking flue gas denitration with the purchase aqueous ammonia outward to can reduce flue gas denitration device running cost, use high-purity ammonia to carry out flue gas denitration, reduce the influence of outside water to the flue gas, reach safety ring protects, energy saving and consumption reduction's purpose.
Description
Technical Field
The utility model belongs to the technical field of the chemical industry, especially, relate to a coking ammonia recycle system.
Background
The flue gas generated by heating the coke oven contains a large amount of sulfur dioxide (SO)2) Nitrogen Oxide (NO)X) And the air is directly discharged into the atmosphere, so that the air environment quality is seriously influenced. At present, coking enterprises adopt' Na2CO3Semi-dry desulfurization and low-temperature SCR selective catalytic reduction denitration dust removal process. Flue gas NO purified by coke ovenxThe discharge concentration is less than 150mg/Nm3(dry basis), SO2The discharge concentration is lower than 30mg/Nm3(dry basis), NH3The discharge concentration is less than 10mg/Nm3(dry basis) particulate matter concentration of less than 15mg/Nm3(dry basis). Denitration system using ammonia (NH)3) Is a reducing agent and reacts with NO in the flue gas under the action of a low-temperature SCR catalystXReaction to produce N2And H2O, to realize NOXRemoval and control of NH3The escape rate of (2). The raw material ammonia used in the SCR denitration process can be generally divided into an outsourcing mode and a self-making mode. The cost for preparing ammonia gas from outsourcing raw material liquid ammonia or 25% ammonia water is higher. However, adoptProcess for producing anhydrous ammonia by ammonium phosphate absorption method to remove tar and acidic component (H)2S、 HCN、CO2) Large investment, large occupied area and complex process, and in the prior art, the ammonia gas is not recycled or is directly discharged into the environment.
SUMMERY OF THE UTILITY MODEL
The utility model provides a solve above-mentioned technical problem and provide a coking ammonia recycle system.
The utility model provides an above-mentioned technical problem's technical scheme as follows: a coking ammonia recycling system comprises a storage tank for storing ammonia water, a first ceramic filter, a tar remover, a first heat exchanger, a deacidification ammonia still, an ammonia gas dephlegmator, a first ammonia gas condensing cooler, a strong ammonia water buffer tank, a second ceramic filter, a strong ammonia water intermediate tank, a second heat exchanger, an ammonia water rectifying tower, a second ammonia gas condensing cooler and an ammonia gas buffer tank;
the outlet of the storage tank is communicated with the inlet of the first ceramic filter through a pipeline, the outlet of the first ceramic filter is communicated with the inlet of the tar remover through a pipeline, the outlet of the tar remover is communicated with the tower-entering ammonia water heat exchange inlet of the first heat exchanger through a pipeline, the tower-entering ammonia water heat exchange outlet of the first heat exchanger is communicated with the inlet of the deacidification ammonia distillation tower through a pipeline, the outlet of the deacidification ammonia distillation tower is communicated with the inlet of the ammonia gas fractional condensation tower through a pipeline, the outlet of the ammonia gas fractional condensation tower is communicated with the inlet of the first ammonia gas condensation cooler through a pipeline, the outlet of the first ammonia gas condensation cooler is communicated with the inlet of the concentrated ammonia water buffer tank through a pipeline, the outlet of the concentrated ammonia water buffer tank is communicated with the inlet of the second ceramic filter through a pipeline, and the outlet of the second ceramic filter is communicated with the inlet of the ammonia water concentrated middle tank through a pipeline, the outlet of the concentrated ammonia water intermediate tank 9 is communicated with the concentrated ammonia water heat exchange inlet of the second heat exchanger through a pipeline, the concentrated ammonia water heat exchange outlet of the second heat exchanger is communicated with the inlet of the ammonia water rectifying tower through a pipeline, the outlet of the ammonia water rectifying tower is communicated with the inlet of the second ammonia condensing cooler through a pipeline, and the outlet of the second ammonia condensing cooler is communicated with the inlet of the ammonia buffer tank through a pipeline.
The utility model has the advantages that: the utility model discloses the ammonia of the effective recycle surplus aqueous ammonia production of product replaces original design and carries out coking flue gas denitration with the purchase aqueous ammonia outward to can reduce flue gas denitration device running cost, use high-purity ammonia to carry out flue gas denitration, reduce the influence of outside water to the flue gas, reach safety ring protects, energy saving and consumption reduction's purpose.
On the basis of the technical scheme, the utility model discloses can also do following improvement.
As the utility model discloses further preferred, the export of tar remover with the intercommunication is provided with the feed pump on the pipeline that the tower aqueous ammonia heat transfer entry that advances of first heat exchanger is linked together.
As the utility model discloses further preferred, the bottom of deacidification ammonia still is equipped with the export of ammonia distillation waste water, be equipped with the import of ammonia distillation waste water heat transfer on the first heat exchanger, the export of ammonia distillation waste water through the pipeline with the import of ammonia distillation waste water heat transfer is linked together, the intercommunication has first delivery pump on the pipeline.
As the utility model discloses it is further preferred, the bottom of ammonia gas dephlegmator is equipped with aqueous ammonia backward flow export, be equipped with aqueous ammonia backward flow import on the deacidification ammonia still, aqueous ammonia backward flow export through the pipeline with the aqueous ammonia backward flow import is linked together.
As the utility model discloses further preferred, the export of strong aqueous ammonia buffer tank with the intercommunication has the second delivery pump on the pipeline that the import of second ceramic filter is linked together.
As the utility model discloses further preferred, the export of strong aqueous ammonia intermediate tank with the intercommunication has the third delivery pump on the pipeline that the strong aqueous ammonia heat transfer entry of second heat exchanger is linked together.
As the utility model discloses further preferred, ammonia water rectification tower bottom is equipped with rectification waste water outlet, be equipped with rectification waste water heat transfer entry on the second heat exchanger, rectification waste water outlet pass through the pipeline with rectification waste water heat transfer entry is linked together.
As the utility model discloses further preferred, still include the backward flow jar, the bottom of second ammonia condensation cooler is equipped with aqueous ammonia backward flow export, aqueous ammonia rectification tower top is equipped with aqueous ammonia backward flow import, aqueous ammonia backward flow export with the aqueous ammonia backward flow import is linked together through the pipeline just the backward flow jar communicates on this pipeline.
Drawings
Fig. 1 is a flow chart of the product system of the present invention.
In the drawings, the components represented by the respective reference numerals are listed below:
1. a first ceramic filter, 2, a tar remover, 3, a first heat exchanger, 4, a deacidification ammonia still, 5, an ammonia gas dephlegmator, 6, a first ammonia gas condensation cooler, 7, a strong ammonia water buffer tank, 8, a second ceramic filter, 9, a strong ammonia water intermediate tank, 10, a second heat exchanger, 11, an ammonia water rectifying tower, 12, a second ammonia gas condensation cooler, 13, a reflux tank, 14, an ammonia gas buffer tank, 15, a storage tank, 16, an ammonia still wastewater heat exchange outlet, 17, an acid gas outlet, 18, a low-pressure steam inlet, 19, a circulating water inlet, 20, a circulating water outlet, 21, a low-temperature water inlet, 22, a low-temperature water outlet, 23, a rectifying wastewater heat exchange outlet, 24, a medium-pressure steam inlet, 25, a high-purity ammonia gas outlet, 26, an ammonia still wastewater heat exchange inlet, 27, a tower inlet ammonia water heat exchange inlet, 28, a tower inlet ammonia water outlet, 29 and a rectifying wastewater heat exchange inlet, 30. concentrated ammonia water heat exchange inlet, 31, concentrated ammonia water heat exchange outlet, 32, feeding pump, 33, ammonia distillation wastewater outlet, 34, first delivery pump, 35, ammonia water reflux outlet, 36, ammonia water reflux inlet, 37, second delivery pump, 38, third delivery pump, 39 and rectification wastewater outlet.
Detailed Description
The principles and features of the present invention are described below in conjunction with the following drawings, the examples given are only intended to illustrate the present invention and are not intended to limit the scope of the present invention.
Examples
As shown in fig. 1, a coking ammonia gas recycling system comprises a storage tank 15 for storing ammonia water, a first ceramic filter 1, a tar remover 2, a first heat exchanger 3, a deacidification ammonia still 4, an ammonia gas dephlegmator 5, a first ammonia gas condensing cooler 6, a strong ammonia water buffer tank 7, a second ceramic filter 8, a strong ammonia water intermediate tank 9, a second heat exchanger 10, an ammonia water rectifying tower 11, a second ammonia gas condensing cooler 12 and an ammonia gas buffer tank 14;
the outlet of the storage tank 15 is communicated with the inlet of the first ceramic filter 1 through a pipeline, the outlet of the first ceramic filter 1 is communicated with the inlet of the tar remover 2 through a pipeline, the outlet of the tar remover 2 is communicated with the tower-entering ammonia water heat exchange inlet 27 of the first heat exchanger 3 through a pipeline, the tower-entering ammonia water heat exchange outlet 28 of the first heat exchanger 3 is communicated with the inlet of the deacidification ammonia distillation tower 4 through a pipeline, the outlet of the deacidification ammonia distillation tower 4 is communicated with the inlet of the ammonia gas fractional condensation tower 5 through a pipeline, the outlet of the ammonia gas fractional condensation tower 5 is communicated with the inlet of the first ammonia gas condensation cooler 6 through a pipeline, the outlet of the first ammonia gas condensation cooler 6 is communicated with the inlet of the concentrated ammonia water buffer tank 7 through a pipeline, the outlet of the concentrated ammonia water buffer tank 7 is communicated with the inlet of the second ceramic filter 8 through a pipeline, the outlet of the second ceramic filter 8 is communicated with the inlet of the concentrated ammonia water intermediate tank 9 through a pipeline, the outlet of the concentrated ammonia water intermediate tank 9 is communicated with the concentrated ammonia water heat exchange inlet 30 of the second heat exchanger 10 through a pipeline, the concentrated ammonia water heat exchange outlet 31 of the second heat exchanger 10 is communicated with the inlet of the ammonia water rectifying tower 11 through a pipeline, the outlet of the ammonia water rectifying tower 11 is communicated with the inlet of the second ammonia condensing cooler 12 through a pipeline, and the outlet of the second ammonia condensing cooler 12 is communicated with the inlet of the ammonia buffer tank 14 through a pipeline.
And a feeding pump 32 is communicated with a pipeline communicated with the tower ammonia water heat exchange inlet 27 of the first heat exchanger 3 at the outlet of the tar remover 2.
The bottom of deacidification ammonia still 4 is equipped with ammonia still waste water export 33, be equipped with ammonia still waste water heat transfer import 26 on the first heat exchanger 3, ammonia still waste water export 33 through the pipeline with ammonia still waste water heat transfer import 26 is linked together, the intercommunication has first delivery pump 34 on the pipeline.
The bottom of ammonia gas dephlegmator 5 is equipped with aqueous ammonia backward flow export 35, be equipped with aqueous ammonia backward flow import 36 on deacidification ammonia still 4, aqueous ammonia backward flow export 35 through the pipeline with aqueous ammonia backward flow import 36 is linked together.
And a second delivery pump 37 is communicated with a pipeline communicated with the outlet of the concentrated ammonia water buffer tank 7 and the inlet of the second ceramic filter 8.
And a third delivery pump 38 is communicated with a pipeline through which the outlet of the strong ammonia water intermediate tank 9 is communicated with the strong ammonia water heat exchange inlet 30 of the second heat exchanger 10.
The bottom of the ammonia water rectifying tower 11 is provided with a rectifying waste water outlet 39, the second heat exchanger 10 is provided with a rectifying waste water heat exchange inlet 29, and the rectifying waste water outlet 39 is communicated with the rectifying waste water heat exchange inlet 29 through a pipeline.
Still include the reflux drum 13, the bottom of second ammonia condensation cooler 12 is equipped with aqueous ammonia backward flow export, aqueous ammonia rectifying column 11 top is equipped with aqueous ammonia backward flow import, aqueous ammonia backward flow export with aqueous ammonia backward flow import is linked together through the pipeline and reflux drum 13 communicates on this pipeline.
The utility model discloses its concrete process of system does:
the residual ammonia water is stored in a storage tank 15, the storage tank 15 is sequentially communicated with a first ceramic filter 1 and a tar remover 2 through pipelines, meanwhile, a lifting pump is communicated on the pipeline communicated with the first ceramic filter 1 of the storage tank 15, the ammonia water after being filtered and removed of impurities through the first ceramic filter 1 is communicated with a first heat exchanger 3 through a pipeline, the ammonia water enters the first heat exchanger 3 through an ammonia water heat exchange inlet 27 of a tower and is discharged from an ammonia water heat exchange outlet 28 of the tower after being heated, meanwhile, the ammonia distillation wastewater generated in a deacidification ammonia distillation tower 4 enters an ammonia distillation wastewater heat exchange inlet 26 on the first heat exchanger 3 through an ammonia distillation wastewater outlet 33, and then enters a biochemical sewage treatment system from an ammonia distillation wastewater heat exchange outlet 16 on the first heat exchanger 3 after being cooled, and the deacidification ammonia distillation tower 4 adopts low-pressure steam entering a low-pressure steam inlet 18 as a heat source to indirectly heat the wastewater at the, the generated steam heats the mixed liquid of each tray of the stripping section of the deacidification ammonia still 4, and the mixed liquid is vaporized into a gas phase after the temperature is raised to the boiling point of ammonia. The working principle of the deacidification ammonia still 4 is as follows: the temperature of weak ammonia water is improved, the solubility in water is reduced, the distillation of the residual ammonia water is realized, the residual ammonia water enters the deacidification ammonia still 4 from the upper tray after passing through the first heat exchanger 3, flows downwards disc by disc along the tray and contacts with steam entering from the bottom of the tower, the temperature of the ammonia water is gradually increased, and the ammonia of the residual ammonia water is continuously evaporated. The steam not only provides a heat source for ammonia distillation, but also increases the partial pressure of water vapor in the tower and reduces the partial pressure of ammonia, thereby accelerating the evaporation speed of ammonia, reducing the ammonia content in the waste liquid at the bottom of the tower and achieving the specified index. The rich ammonia gas is extracted from the side line of the tower (namely is discharged from the outlet of the deacidification ammonia distillation tower 4), and the acid gas separated from the tower top enters the acid gas outlet 17 to be discharged and collected.
The acid gas at the top of the deacidification ammonia still 4 is communicated with the desulfuration precooling tower through an acid gas outlet 17 by a pipeline. The ammonia gas taken out in the side line of the tower, i.e., discharged through the outlet of the deacidification ammonia still 4, is condensed by an ammonia gas condenser 5. The ammonia gas dephlegmator 5 is a cooler, ammonia gas is cooled by circulating water (a circulating water inlet 19 enters from the lower part of the ammonia gas dephlegmator 5 and flows out from a circulating water outlet 20 at the upper part of the ammonia gas dephlegmator 5, the temperature of the ammonia gas is reduced to 92 ℃ from 101 ℃, the circulating water flows out of a tube pass, the ammonia gas flows out of a shell pass), liquid phase backflow participates in vapor-liquid phase mass transfer, uncondensed vapor phase continuously enters a first ammonia gas condensation cooler 6, the ammonia gas is cooled into concentrated ammonia water with the temperature of more than 20 percent (wt percent) by low-temperature water (the first ammonia gas condensation cooler 6 can be a tube heat exchanger, the ammonia gas flows out of the shell pass, the low-temperature water flows out of the tube pass, a low-temperature water inlet 21 (a tube pass inlet) enters from the lower part, a.
Then, the concentrated ammonia water is filtered again by the second ceramic filter 8 and passes through the second heat exchanger 10 (the concentrated ammonia water enters the second heat exchanger 10 through the concentrated ammonia water heat exchange inlet 30 to be heated and then is discharged through the concentrated ammonia water heat exchange outlet 31, meanwhile, the rectification wastewater generated after rectification by the ammonia water rectification tower 11 is discharged through the rectification wastewater outlet 39, enters the rectification wastewater heat exchange inlet 29 through a pipeline, finally enters the second heat exchanger 10 to be cooled and then is discharged from the rectification wastewater heat exchange outlet 23 arranged at the top of the second heat exchanger 10).
The bottom of the ammonia water rectifying tower 11 is provided with a medium-pressure steam inlet 24, and steam is used as stripping steam of the strong ammonia water after entering the ammonia water rectifying tower 11. In an ammonia water rectifying tower 11, ammonia water is heated and distilled by 1.6MPa superheated steam entering from a medium-pressure steam inlet 24 at the bottom of the tower, ammonia gas (the concentration is 99.8%) escaping from the top of the ammonia water rectifying tower 11 is partially condensed into liquid ammonia by a second condensing cooler 12 (the second condensing cooler 12 is a tubular heat exchanger, an ammonia gas shell pass, low-temperature water enters from the bottom of the second condensing cooler 12 through a low-temperature water inlet 21 (a tubular pass inlet), a low-temperature water outlet 22 (a tubular pass outlet) flows out from the top of the second condensing cooler 12, the temperature of the ammonia gas is reduced from 40 ℃ to 30 ℃), and the ammonia water in the second condensing cooler 12 enters the ammonia water rectifying tower 11 by a reflux tank 13, guarantee 11 backward flow of aqueous ammonia rectifying column is stable, and the ammonia is equipped with high-purity ammonia export 25 on slow jar 14, and high-purity ammonia export 25 exhaust ammonia passes through the pipeline intercommunication with coking flue gas denitration, in addition the utility model discloses the product equipment that the product used is current product equipment.
The utility model discloses the ammonia of the production of the effective recycle surplus aqueous ammonia of product replaces original design and carries out coking flue gas denitration with the purchase aqueous ammonia outward to can reduce flue gas denitration device running cost, use high-purity ammonia to carry out flue gas denitration, reduce the influence of outside water to the flue gas.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplicity of description, and do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore should not be construed as limiting the present invention.
Furthermore, in the description of the present invention, the term "plurality" means at least two, e.g., two, three, etc., unless explicitly limited otherwise.
The above description is only for the preferred embodiment of the present invention, and is not intended to limit the present invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. A coking ammonia gas recycling system is characterized by comprising a storage tank (15) for storing ammonia water, a first ceramic filter (1), a tar remover (2), a first heat exchanger (3), a deacidification ammonia still (4), an ammonia gas dephlegmator (5), a first ammonia gas condensing cooler (6), a concentrated ammonia water buffer tank (7), a second ceramic filter (8), a concentrated ammonia water intermediate tank (9), a second heat exchanger (10), an ammonia water rectifying tower (11), a second ammonia gas condensing cooler (12) and an ammonia gas buffer tank (14);
the outlet of the storage tank (15) is communicated with the inlet of the first ceramic filter (1) through a pipeline, the outlet of the first ceramic filter (1) is communicated with the inlet of the tar remover (2) through a pipeline, the outlet of the tar remover (2) is communicated with the tower-entering ammonia water heat exchange inlet (27) of the first heat exchanger (3) through a pipeline, the tower-entering ammonia water heat exchange outlet (28) of the first heat exchanger (3) is communicated with the inlet of the deacidification ammonia still tower (4) through a pipeline, the outlet of the deacidification ammonia still tower (4) is communicated with the inlet of the ammonia gas dephlegmator (5) through a pipeline, the outlet of the ammonia gas dephlegmator (5) is communicated with the inlet of the first ammonia gas condensation cooler (6) through a pipeline, the outlet of the first ammonia gas condensation cooler (6) is communicated with the inlet of the concentrated ammonia water buffer tank (7) through a pipeline, the outlet of the concentrated ammonia water buffer tank (7) is communicated with the inlet of the second ceramic filter (8) through a pipeline, the outlet of the second ceramic filter (8) is communicated with the inlet of the concentrated ammonia water intermediate tank (9) through a pipeline, the outlet of the concentrated ammonia water intermediate tank (9) is communicated with the concentrated ammonia water heat exchange inlet (30) of the second heat exchanger (10) through a pipeline, the concentrated ammonia water heat exchange outlet (31) of the second heat exchanger (10) is communicated with the inlet of the ammonia water rectifying tower (11) through a pipeline, the outlet of the ammonia water rectifying tower (11) is communicated with the inlet of the second ammonia condensing cooler (12) through a pipeline, and the outlet of the second ammonia condensing cooler (12) is communicated with the inlet of the ammonia gas buffer tank (14) through a pipeline.
2. The coking ammonia gas recycling system of claim 1, characterized in that a feed pump (32) is arranged on a pipeline of the outlet of the tar remover (2) communicated with the tower-entering ammonia water heat exchange inlet (27) of the first heat exchanger (3).
3. The coking ammonia gas recycling system according to claim 1, characterized in that an ammonia distillation wastewater outlet (33) is arranged at the bottom of the deacidification ammonia distillation tower (4), an ammonia distillation wastewater heat exchange inlet (26) is arranged on the first heat exchanger (3), the ammonia distillation wastewater outlet (33) is communicated with the ammonia distillation wastewater heat exchange inlet (26) through a pipeline, and the pipeline is communicated with a first delivery pump (34).
4. A coking ammonia gas recycling system according to any one of claims 1 to 3, characterized in that the ammonia gas dephlegmator (5) is provided with an ammonia water reflux outlet (35) at the bottom, the deacidification ammonia still (4) is provided with an ammonia water reflux inlet (36), and the ammonia water reflux outlet (35) is communicated with the ammonia water reflux inlet (36) through a pipeline.
5. The coking ammonia gas recycling system according to any one of claims 1 to 3, characterized in that a second delivery pump (37) is communicated with a pipeline connecting an outlet of the concentrated ammonia water buffer tank (7) and an inlet of the second ceramic filter (8).
6. The coking ammonia gas recovery and utilization system according to any one of claims 1 to 3, characterized in that a third delivery pump (38) is communicated with a pipeline for communicating an outlet of the concentrated ammonia water intermediate tank (9) with the concentrated ammonia water heat exchange inlet (30) of the second heat exchanger (10).
7. The coking ammonia gas recycling system according to any one of claims 1 to 3, characterized in that the bottom of the ammonia water rectifying tower (11) is provided with a rectifying wastewater outlet (39), the second heat exchanger (10) is provided with a rectifying wastewater heat exchange inlet (29), and the rectifying wastewater outlet (39) is communicated with the rectifying wastewater heat exchange inlet (29) through a pipeline.
8. The coking ammonia gas recycling system according to any one of claims 1 to 3, further comprising a reflux tank (13), wherein an ammonia water reflux outlet is arranged at the bottom of the second ammonia condensing cooler (12), an ammonia water reflux inlet is arranged at the top of the ammonia water rectifying tower (11), the ammonia water reflux outlet is communicated with the ammonia water reflux inlet through a pipeline, and the reflux tank (13) is communicated with the pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920873621.9U CN210752112U (en) | 2019-06-11 | 2019-06-11 | Coking ammonia recycle system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920873621.9U CN210752112U (en) | 2019-06-11 | 2019-06-11 | Coking ammonia recycle system |
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| CN210752112U true CN210752112U (en) | 2020-06-16 |
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| CN201920873621.9U Active CN210752112U (en) | 2019-06-11 | 2019-06-11 | Coking ammonia recycle system |
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| CN (1) | CN210752112U (en) |
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