CN112499647A - Hydrogen recovery process - Google Patents
Hydrogen recovery process Download PDFInfo
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- CN112499647A CN112499647A CN202011546062.4A CN202011546062A CN112499647A CN 112499647 A CN112499647 A CN 112499647A CN 202011546062 A CN202011546062 A CN 202011546062A CN 112499647 A CN112499647 A CN 112499647A
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- hydrogen
- gas
- ammonia
- purge gas
- hydrogen recovery
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- 239000001257 hydrogen Substances 0.000 title claims abstract description 120
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 120
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 115
- 238000011084 recovery Methods 0.000 title claims abstract description 43
- 239000007789 gas Substances 0.000 claims abstract description 110
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 101
- 238000010926 purge Methods 0.000 claims abstract description 57
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 38
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 14
- 239000002994 raw material Substances 0.000 claims abstract description 14
- 238000003860 storage Methods 0.000 claims abstract description 9
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 8
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 8
- 238000000034 method Methods 0.000 claims abstract description 7
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 7
- 238000002360 preparation method Methods 0.000 claims abstract description 5
- 238000001816 cooling Methods 0.000 claims abstract description 4
- 230000002194 synthesizing effect Effects 0.000 claims abstract description 4
- 239000012528 membrane Substances 0.000 claims description 43
- 239000007788 liquid Substances 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 7
- 239000000126 substance Substances 0.000 abstract description 4
- 238000005406 washing Methods 0.000 description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 11
- 238000000926 separation method Methods 0.000 description 10
- 238000004519 manufacturing process Methods 0.000 description 8
- 239000012466 permeate Substances 0.000 description 6
- 239000003337 fertilizer Substances 0.000 description 4
- 239000008234 soft water Substances 0.000 description 4
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 3
- 235000011114 ammonium hydroxide Nutrition 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000010276 construction Methods 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 238000004364 calculation method Methods 0.000 description 2
- 230000006837 decompression Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 description 1
- 239000004254 Ammonium phosphate Substances 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 230000002159 abnormal effect Effects 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- 229910000148 ammonium phosphate Inorganic materials 0.000 description 1
- 235000019289 ammonium phosphates Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- -1 nitrogen-containing compound Chemical class 0.000 description 1
- 238000011056 performance test Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/04—Preparation of ammonia by synthesis in the gas phase
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/501—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by diffusion
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Analytical Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The application relates to the field of chemical industry, and particularly discloses a hydrogen recovery process, which comprises the following steps of S1, preparing raw material gas by adopting hydrogen and nitrogen, and synthesizing ammonia gas in a synthesis tower; s2, cooling the gas ammonia to obtain liquid ammonia, injecting the liquid ammonia into a liquid ammonia storage tank under reduced pressure, and separating out purge gas from the liquid ammonia in the process of reducing the pressure; s3, introducing the purge gas into a hydrogen recovery system to recover hydrogen in the purge gas; and S4, pressurizing the recovered hydrogen and circulating the hydrogen to the preparation of the raw material gas. The hydrogen recovery process has the advantage of improving the utilization rate of hydrogen.
Description
Technical Field
The present application relates to the field of ammonia synthesis technology, and more particularly, it relates to a hydrogen recovery process.
Background
Ammonia is one of important inorganic chemical products and plays an important role in national economy. Besides the liquid ammonia can be directly used as fertilizer, the nitrogen fertilizers used in agriculture, such as urea, ammonium nitrate, ammonium phosphate, ammonium chloride and various nitrogen-containing compound fertilizers, are all prepared from ammonia. Therefore, synthetic ammonia plays an important role in national economy, and the worldwide annual synthetic ammonia yield reaches more than 1 hundred million tons, wherein about 80 percent of ammonia is used for producing chemical fertilizers, and 20 percent of ammonia is used as a raw material of other chemical products.
As is well known, synthetic ammonia is directly synthesized by nitrogen and hydrogen under high temperature, high pressure and a catalyst, and after cooling, liquid ammonia is separated from gas and enters a liquid ammonia storage tank under reduced pressure; with the pressure decrease, the hydrogen and nitrogen dissolved in the liquid ammonia at high pressure are decomposed from the liquid ammonia, and this gas is also called purge gas.
However, in the existing production process, the purge gas is combusted after a part of ammonia is recovered by the isobaric tower, and hydrogen is also combusted and consumed as raw material gas for ammonia synthesis, so that the waste of hydrogen is caused.
Disclosure of Invention
In order to improve the utilization rate of hydrogen, the application provides a hydrogen recovery process.
The technical scheme is that the hydrogen recovery process comprises the following steps:
s1, preparing raw material gas by adopting hydrogen and nitrogen, and synthesizing ammonia in a synthesis tower;
s2, cooling the gas ammonia to obtain liquid ammonia, injecting the liquid ammonia into a liquid ammonia storage tank under reduced pressure, and separating out purge gas from the liquid ammonia in the process of reducing pressure;
s3, introducing the purge gas into a hydrogen recovery system to recover hydrogen in the purge gas;
and S4, pressurizing the recovered hydrogen and circulating the hydrogen to the preparation of the raw material gas.
By adopting the technical scheme, in the pressure reduction process, the purge gas separated out from the liquid ammonia can be recycled by the hydrogen recovery system, and the recycled hydrogen is further recycled to the configuration of the feed gas and is used as part of source gas of the hydrogen in the feed gas, so that the effects of saving energy and improving the utilization rate of the feed gas are obtained; in addition, in the present application, only the hydrogen recovery system is needed to recover and reuse the hydrogen in the purge gas to the feed gas.
Preferably, the hydrogen recovery system comprises an ammonia washing tower, a gas-liquid separator and at least two groups of hydrogen membrane separators which are sequentially connected through pipelines.
By adopting the technical scheme, the ammonia washing tower can recollect part of ammonia mixed with the purge gas, so that the utilization rate of raw materials is further improved; the gas-liquid separator can separate the liquid ammonia and the purge gas to improve the purity of the purge gas; the hydrogen in the purge gas can be separated from other gases by at least two groups of hydrogen membrane separators, so that purer hydrogen is obtained and the recovery rate of the hydrogen is improved; in addition, the hydrogen membrane separator has simple process flow, no moving parts and few control parts, is suitable for continuous production, ensures that the operating rate can reach 100 percent and has high economic benefit.
Preferably, the pressure of purge gas introduced into the hydrogen membrane separator is 1.5-1.6MPa, and the gas amount is 500Nm3/h。
By adopting the technical scheme, the pressure of the purge gas introduced into the hydrogen membrane separator is 1.5-1.6Mpa, so that the hydrogen can be separated by the system under lower pressure, thereby saving energy and improving the safety of the system.
Preferably, the pressure of purge gas introduced into the hydrogen membrane separator is 1.5MPa, and the gas amount is 500Nm3/h。
Preferably, the hydrogen recovery system further comprises a jacket heater connected between the gas-liquid separator and the hydrogen membrane separator by a pipe.
By adopting the technical scheme, the sleeve heater can heat the purge gas, so that on one hand, the movement among gas molecules can be accelerated, and the separation degree of each gas in the purge gas is improved; on the other hand, the water condensation in a saturated state is prevented, so that the membrane separation efficiency is prevented from being influenced, and the hydrogen recovery rate is further influenced.
Preferably, the heating temperature of the sleeve heater is 45-50 ℃.
By adopting the technical scheme, on one hand, the movement among gas molecules can be accelerated by heating to 45-50 ℃, and the separation degree of each gas in the purge gas is improved; on the other hand, the water condensation in a saturated state is prevented, so that the membrane separation efficiency is prevented from being influenced, and the hydrogen recovery rate is further influenced.
Preferably, the heating temperature of the sleeve heater is 48 ℃.
By adopting the technical scheme, the damage of the gas temperature of about 48 ℃ to the low-pressure membrane is small, the damage of the seal head in the hydrogen membrane separator and the failure of the silk membrane are prevented, and the production safety is improved.
Preferably, the hydrogen recovery system further comprises a pipe filter connected between the jacket heater and the hydrogen membrane separator by a pipe.
By adopting the technical scheme, the pipeline filter can remove impurities such as rust in gas, improve the purity of the purge gas and reduce the damage to the low-pressure membrane.
Preferably, the purge gas comprises 47% to 49% hydrogen.
By adopting the technical scheme, the hydrogen in the purge gas occupies 47-49 percent, so the purge gas introduced into the hydrogen membrane separator is hydrogen-rich gas, and can be used in a low-pressure state; in addition, membrane separation is economical.
In summary, the present application has the following beneficial effects:
1. because this application adopts hydrogen recovery system, the purge gas that produces in the synthetic ammonia is through low pressure membrane separation, has obtained the high recovered gas of hydrogen content, and the hydrogen after the purification is as the raw materials of enterprise production synthetic ammonia, promotes the utilization ratio of hydrogen, reduces the raw coal consumption that is used for preparing hydrogen from the source, promotes the effect.
2. The pressure of the purge gas introduced into the hydrogen membrane separator is 1.5-1.6Mpa, so that the hydrogen can be separated by the system under lower pressure, thereby saving energy and improving the safety of the system.
Drawings
FIG. 1 is a flow diagram of a hydrogen recovery system provided herein.
Description of reference numerals: 1. an ammonia washing tower; 2. a water storage tank; 3. a high pressure water pump; 4. a gas-liquid separator; 5. a sleeve heater; 6. a pipeline filter; 7. a hydrogen membrane separator.
Detailed Description
The present application will be described in further detail with reference to the following drawings and examples.
Examples
An ammonia synthesis process, comprising the following steps,
s1, preparing raw material gas by adopting hydrogen and nitrogen, and synthesizing ammonia in a synthesis tower;
s2, sending the gas ammonia into an ammonia condensing tower to be cooled to obtain liquid ammonia, decompressing the liquid ammonia and injecting the liquid ammonia into a liquid ammonia storage tank, and separating out purge gas from the liquid ammonia in the decompression process;
s3, introducing the purge gas into a hydrogen recovery system to recover hydrogen in the purge gas;
and S4, pressurizing the recovered hydrogen and circulating the hydrogen to the preparation of the raw material gas.
The hydrogen recovery system comprises an ammonia washing tower 1, a gas-liquid separator 4, a sleeve heater 5, a pipeline filter 6 and two groups of hydrogen membrane separators 7 which are connected in sequence through pipelines; the ammonia washing tower 1 is also connected with a water storage tank 2 through a pipeline, and soft water in the water storage tank 2 is conveyed to a spraying position at the top of the ammonia washing tower 1 through a high-pressure water pump 4.
Wherein the heating temperature of the sleeve heater 5 is 45-50 ℃; the pressure of the purge gas introduced into the membrane separator is 1.5-1.6Mpa, and the gas flow is 500Nm3/h。
Specifically, the purge gas with entrained gas ammonia is firstly sent into an ammonia washing tower 1, meanwhile, soft water in a water storage tank 2 is conveyed to the ammonia washing tower 1 through a high-pressure water pump 3, synthetic ammonia is sprayed by the soft water and then dissolved in the soft water to form ammonia water, and the ammonia water is collected and prepared.
The rest of the purge gas is discharged from the ammonia washing tower 1 and is introduced into a gas-liquid separator 4, the ammonia is further separated, and the waste water is discharged to a trench.
Further, the purge gas is heated to 50 ℃ by a sleeve heater 5 to prevent water condensation in a saturated state in the purge gas;
further, the purge gas is introduced into a pipeline filter 6 to remove impurities such as rust in the gas; and the temperature of the purge gas is kept between 45 and 50 ℃ by keeping the temperature of the pipeline at the temperature.
Further, the purge gas passes through two groups of hydrogen membrane separators 7 in turn, the pressure of the purge gas introduced into the hydrogen membrane separators 7 is controlled to be 1.5-1.6MPa, and the gas flow is controlled to be 500Nm3H; and the temperature of the purge gas is kept at 50 ℃ by keeping the temperature of the pipeline at the temperature.
On one hand, permeate gas containing hydrogen is obtained through separation, and the permeate gas is pressurized again and circulated to the preparation of feed gas, so that the utilization rate of the hydrogen is improved; on the other hand, high-pressure waste gas obtained by separation is sent into an incinerator for incineration after being decompressed by a decompression valve.
Because the membrane component in the hydrogen membrane separator 7 is made of high molecular materials, the pressure resistance of the membrane component has certain limitation, and the damage of the seal head and the failure of the silk membrane can be caused by overhigh temperature and pressure difference. Therefore, detection and self-control are very important.
In the application, the hydrogen recovery system is controlled by a tail gas automatic regulating valve, the set value is 1.6MPa, when the system gas amount shows that the pressure is reduced, the regulating valve is automatically closed, the system pressure is maintained to be stable, the normal operation of the hydrogen membrane separator 7 is ensured, and the pressure set value can be adjusted according to the actual working condition on site.
The inlet of the ammonia washing tower 1 of the hydrogen recovery system adopts a manual regulating valve, and when the air input of the system is controlled and the system is in an abnormal condition, the valve is automatically closed, and the connection between the system and the outside is cut off, so that the safety of the hydrogen membrane separator 7 is ensured.
The automatic control system performs automatic control operation on the pressure of the ammonia washing tower 1, the liquid level of ammonia water, the discharge capacity of vent gas, the heating temperature and the like, and simultaneously performs automatic alarm and interlocking shutdown on the liquid level exceeding, overpressure, overtemperature and the like, and the membrane separation device can automatically enter a self-protection state after shutdown.
Performance test
Hydrogen recovery rate calculation formula:
with on-site flow meter and manual analysis eta =
x100%
In the formula: xd-hydrogen content in the permeate gas; f-purge flow; w-exhaust gas flow; xf-hydrogen content in purge gas.
And respectively taking the three production data, and obtaining the hydrogen recovery rate through a hydrogen recovery rate calculation formula, wherein the hydrogen recovery rate is as follows:
1. pressure of purge gas introduced into the hydrogen membrane separator: 1.5 MPa; purge flow rate: 160NM3H; flow rate of tail gas: 82 NM3/h；
Hydrogen content in purge gas: 49 percent; hydrogen content in the permeate gas: 87%, resulting in a hydrogen recovery: 86.56 percent.
2. Pressure of purge gas introduced into the hydrogen membrane separator: 1.55MPa, purge flow: 180 NM3H; flow rate of tail gas: 99NM3/h；
Hydrogen content in purge gas: 47%; hydrogen content in the permeate gas: 89.5%, obtaining hydrogen recovery: 85.69 percent.
3. Pressure of purge gas introduced into the hydrogen membrane separator: 1.6 MPa; purge flow rate: 140NM3H; flow rate of tail gas: 75NM3/h；
Hydrogen content in purge gas: 48.6 percent; hydrogen content in the permeate gas: 90.8%, hydrogen recovery: 86.74 percent.
Analysis of results
The hydrogen recovery rate obtained after three times of sampling is uniform>85 percent of the total hydrogen membrane separation process, and the main reason is that the membrane entering pressure is lower, so that the pressure difference at two sides of the hydrogen membrane separator is reduced, the driving force of the permeation gas is reduced, the influence of the actual treatment capacity of the hydrogen membrane separator is utilized, the gas quantity of the raw material gas is properly reduced under the existing production condition, and the raw material gas quantity is maintained at 150 NM3About/h, and simultaneously, the operation temperature is increased to 50 ℃, so that the problem that the service life is influenced by too large gas passing amount of the hydrogen membrane separator is avoided.
In addition, the investment cost of the early-stage production of the application is 45 ten thousand yuan, the installation cost is 15 ten thousand yuan, and the total investment of the engineering construction and the construction investment of the construction engineering is 61.5 ten thousand yuan.
In the daily production process, the flow rate of purge gas is 500m3Calculated by 8000 hours of production all the year, the total amount reaches 180 ten thousand meters3. The hydrogen unit price is about 1.1 yuan/m calculated according to the cost of the semi-water gas prepared by the fixed bed3Therefore, the economic benefit can be generated 198 ten thousand yuan throughout the year, and the cost can be recovered in 4 months.
The present embodiment is only for explaining the present application, and it is not limited to the present application, and those skilled in the art can make modifications of the present embodiment without inventive contribution as needed after reading the present specification, but all of them are protected by patent law within the scope of the claims of the present application.
Claims (9)
1. A hydrogen recovery process is characterized by comprising the following steps,
s1, preparing raw material gas by adopting hydrogen and nitrogen, and synthesizing ammonia in a synthesis tower;
s2, cooling the gas ammonia to obtain liquid ammonia, injecting the liquid ammonia into a liquid ammonia storage tank under reduced pressure, and separating out purge gas from the liquid ammonia in the process of reducing pressure;
s3, introducing the purge gas into a hydrogen recovery system to recover hydrogen in the purge gas;
and S4, pressurizing the recovered hydrogen and circulating the hydrogen to the preparation of the raw material gas.
2. The hydrogen recovery process according to claim 1, wherein the hydrogen recovery system comprises an ammonia scrubber (1), a gas-liquid separator (4) and at least two sets of hydrogen membrane separators (7) connected in sequence by pipes.
3. The hydrogen recovery process according to claim 2, wherein the purge gas is introduced into the hydrogen membrane separator (7) at a pressure of 1.5 to 1.6MPa and at a gas rate of 500Nm3/h。
4. Process for ammonia synthesis according to claim 3, characterized in that the purge gas is fed into the hydrogen membrane separator (7) at a pressure of 1.5MPa and at a gas rate of 500Nm3/h。
5. The hydrogen recovery process according to claim 2, wherein the hydrogen recovery system further comprises a jacket heater (5), and the jacket heater (5) is connected between the gas-liquid separator (4) and the hydrogen membrane separator (7) by a pipe.
6. The hydrogen recovery process according to claim 4, wherein the heating temperature of the jacket heater (5) is 45-50 ℃.
7. The hydrogen recovery process of claim 4, wherein the heating temperature of the thimble heater is 48 ℃.
8. A hydrogen recovery process according to claim 1, characterized in that the hydrogen recovery system further comprises a pipe filter (6), the pipe filter (6) being connected by pipe between the thimble heater (5) and the hydrogen membrane separator (7).
9. The hydrogen recovery process of claim 1, wherein the purge gas comprises 47% to 49% hydrogen.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011546062.4A CN112499647A (en) | 2020-12-23 | 2020-12-23 | Hydrogen recovery process |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202011546062.4A CN112499647A (en) | 2020-12-23 | 2020-12-23 | Hydrogen recovery process |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040219088A1 (en) * | 2003-04-29 | 2004-11-04 | Harvey Wen | Mini ammonia plant |
| CN101531347A (en) * | 2008-03-11 | 2009-09-16 | 中国石油大学(北京) | Method for recycling and synthesizing nitrogen and hydrogen in off-gases of ammonia and device thereof |
| CN101948121A (en) * | 2010-09-19 | 2011-01-19 | 昆明理工大学 | Ammonia synthesis technology |
| CN102985367A (en) * | 2010-04-07 | 2013-03-20 | 阿梅尼亚·卡萨莱股份有限公司 | Hydrogen and nitrogen recovery from ammonia purge gas |
| CN203392841U (en) * | 2013-07-11 | 2014-01-15 | 新疆天运化工有限公司 | Recovery device of hydrogen for preparing synthetic ammonia |
-
2020
- 2020-12-23 CN CN202011546062.4A patent/CN112499647A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040219088A1 (en) * | 2003-04-29 | 2004-11-04 | Harvey Wen | Mini ammonia plant |
| CN101531347A (en) * | 2008-03-11 | 2009-09-16 | 中国石油大学(北京) | Method for recycling and synthesizing nitrogen and hydrogen in off-gases of ammonia and device thereof |
| CN102985367A (en) * | 2010-04-07 | 2013-03-20 | 阿梅尼亚·卡萨莱股份有限公司 | Hydrogen and nitrogen recovery from ammonia purge gas |
| CN101948121A (en) * | 2010-09-19 | 2011-01-19 | 昆明理工大学 | Ammonia synthesis technology |
| CN203392841U (en) * | 2013-07-11 | 2014-01-15 | 新疆天运化工有限公司 | Recovery device of hydrogen for preparing synthetic ammonia |
Non-Patent Citations (2)
| Title |
|---|
| 毛应淮等: "制氨", pages 444 * |
| 陈观文等: "《分离膜应用于工程案例》", 国防工业出版社, pages: 386 - 387 * |
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