CN103663367B - Method for recovering hydrogen and ammonia in synthetic ammonia exhausted gas - Google Patents
Method for recovering hydrogen and ammonia in synthetic ammonia exhausted gas Download PDFInfo
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- CN103663367B CN103663367B CN201310699052.8A CN201310699052A CN103663367B CN 103663367 B CN103663367 B CN 103663367B CN 201310699052 A CN201310699052 A CN 201310699052A CN 103663367 B CN103663367 B CN 103663367B
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Abstract
The method discloses a method for recovering hydrogen and ammonia in synthetic ammonia exhausted gas. The method comprises a pretreatment process, a membrane separation process and an ammonia recovering process; and an ammonia resistant membrane which can tolerate an ammonia gas phase with concentration lower than 6% (v/v) for a long time is adopted to treat the synthetic ammonia exhausted gas, hydrogen and most ammonia in the synthetic ammonia exhausted gas are recovered, and then ammonia contained in retention gas after membrane separation is recovered with methods of water washing and ammonia distillation and changed into a liquid ammonia product. According to the method for recovering hydrogen and ammonia in the synthetic ammonia exhausted gas, safe and stable operation of the membrane separation process is guaranteed essentially, and more than 85% of hydrogen and more than 75% of ammonia can be recovered; equipment investment and occupied land involved in the ammonia recovering process are reduced by 60%; and meanwhile, energy consumption of an ammonia absorption tower and an ammonia still is reduced by 70%-80%, and the operation cost is reduced by 70%-80%.
Description
Technical field
The invention belongs to the technical field that synthetic ammonia periodic off-gases reclaims, particularly relate to a kind of method of recover hydrogen and ammonia from synthetic ammonia periodic off-gases.
Background technology
In production of synthetic ammonia, hydrogen and nitrogen are the raw materials of synthetic ammonia.Nitrogen is generally separated from air, and hydrogen is generally obtained by conversion of natural gas or gasification, and hydrogen and nitrogen react under higher pressure and temperature and under catalyst action produces ammonia.Be subject to the restriction of chemical equilibrium, reactant can not transform completely, and unreacted nitrogen and hydrogen enter synthetic tower again and carries out ammonia synthesis reaction after recycle compressor mixes with the virgin gas of supplementing.Because synthetic ammonia feedstock nitrogen and hydrogen all contain a certain amount of inert component argon gas and methane, these inert components are constantly accumulated in working cycle, not only consume loop compression merit, the useful volume of synthetic tower also can be made to reduce, also can affect the normal reaction of synthetic ammonia, so synthetic tower mixed gas must discharge a part of gas, to control the concentration of inert component argon gas and methane in synthetic tower, this part discharge gas is called synthetic ammonia periodic off-gases.Discharge tolerance is about ~ 300Nm
3/ ton ammonia, the classical group of this gas becomes: H250 ~ 70%(V/V), NH
31 ~ 6%(V/V), N
218 ~ 25%(V/V), remaining is methane and argon gas.
Membrane separation technique is mostly adopted to fold into hydrogen and ammonia in ammonia relief gas back and forth at present.Due to the non-constant of the tolerance of current mould material to ammonia, so high pressure periodic off-gases must remove ammonia by pre-treatment before entering membrane separation apparatus, its method is generally employing high-pressure washing, in ammonia absorber, ammonia is removed, control the volume content less than 0.02% of ammonia in gas phase, and then the hydrogen entered in membrane separation apparatus recovery periodic off-gases, the infiltration gas of film is the hydrogen of enriching and recovering, turn back to synthesis system, the impermeable gas of film is mainly methane, nitrogen, argon gas and a small amount of hydrogen, uses as fuel.Aforesaid method is very strict to the operational requirement of ammonia absorber, can not occur that in gas phase, ammonia density exceeds standard, more definitely will avoid the generation occurring entrainment and Concerning Flooding Phenomenon, otherwise can cause the expendable damage of downstream separation film.In the application process of reality, because ammonia absorber operation goes wrong, the example causing separatory membrane to damage is very many.
Summary of the invention
The object of the present invention is to provide a kind of technical process simple, energy consumption is low, easy to operate, operating safety, the method for hydrogen and ammonia in synthetic ammonia periodic off-gases; Another object is to provide a kind of device for realizing hydrogen and ammonia in described synthetic ammonia periodic off-gases.
The present invention adopt can withstand long term exposure ammonia phase concentration be less than 6%(V/V) resistant to ammonia film process synthetic ammonia periodic off-gases, reclaim hydrogen wherein and most of ammonia, then adopt the method for washing and ammonia still process, reclamation film retains the ammonia contained in gas after being separated, and is become liquefied ammonia product.The method of recover hydrogen and ammonia from synthetic ammonia periodic off-gases of the present invention, its key step comprises preprocessing process, membrane separating process and ammonia recovering process;
Described preprocessing process: synthetic ammonia periodic off-gases first through strainer removing solid particulate and drop, then after gas-gas heat exchanger progressively heats up, is warmed up to 45 ~ 90 DEG C by well heater; Wherein, 1. described through strainer removing solid particulate and drop, be conducive to preventing mechanical impurity from entering separatory membrane, be conducive to the separation performance and the work-ing life that ensure film; 2. continuously across gas-gas heat exchanger, not only the temperature of ammonia relief gas is raised, can also reclaim and be separated membrane permeate gas and the heat retaining gas.3. the well heater in described preprocessing process, its thermal source can be steam, deep fat, electricity or other high-temperature medium; Use well heater to improve gas and enter film temperature, ensure that gas departs from its dew-point temperature more than 5 ~ 20 DEG C, to have prevented liquid from condensing on film, cause the damage of film.
Described membrane separating process: through the gas of preprocessing process process, after separatory membrane process, the gas of the per-meate side enrichment of separatory membrane, after the gas-gas heat exchanger cooling in preprocessing process, is reclaimed by synthetic compressor; The gas retaining lateral enrichment of separatory membrane, after the gas-gas heat exchanger cooling in preprocessing process, enters hydrogen and ammonia recovering process; Wherein, 1. the material behavior of this separatory membrane be hydrogen and ammonia all preferential through, in the per-meate side enrichment of separatory membrane, then deliver to synthetic compressor entrance, turn back to ammonia synthesis system, realize the recovery of the hydrogen of more than 85% and the ammonia of more than 75%.Separatory membrane retain side be enrich methane, argon gas, nitrogen and residue ammonia gas.2. after membrane separating process, the hydrogen of more than 85% and the ammonia of more than 75% are recycled utilization, but retaining in gas of separatory membrane still contains a certain amount of ammonia, and these gases all use as fuel gas usually.But due to the existence of ammonia, the content overproof of NOx in the gas after burning can be caused, also result in the loss of ammonia simultaneously.Reclaim with the form of liquefied ammonia so the present invention adopts the way of ammonia absorption and ammonia still process film to be retained the ammonia in gas, thus realize the recovery of ammonia nearly 100% in synthetic ammonia periodic off-gases.
Described ammonia recovering process: the synthetic ammonia periodic off-gases after membrane separating process process, enters from the bottom of ammonia absorber, upruss, after ammonia absorber washing removing ammonia, delivers to fuel gas system; By the ammonia soln obtained bottom ammonia absorber, after interchanger is warmed up to 150 ~ 190 DEG C, enter ammonia still process.Wherein, in the ammonia soln obtained bottom ammonia absorber, the concentration of ammonia is 5 ~ 20wt%.In ammonia still, realize being separated of ammonia and water, obtain purity at tower top and be greater than 99.5wt% liquefied ammonia product, at the bottom of tower, obtain the aqueous solution that ammonia density is less than 200ppmw, then return it to ammonia absorber recycle by high-pressure pump.
For technique scheme, in the preferred case, described separation membrane material is polyaramide.Because the NH3 content in periodic off-gases is generally 1 ~ 6%(V/V), conventional mould material, as polyimide, polysulfones all can not tolerate so high ammonia concentration, so adopt the separatory membrane of polyaramid materials in the present invention, this material can be less than 6%(V/V at ammonia phase concentration) condition under, life-time service.
For technique scheme, in the preferred case, the gas-gas heat exchanger in described preprocessing process is 3 series connection; The separatory membrane of described membrane separating process is 2 series connection; The infiltration gas of first step separatory membrane is after second gas-gas heat exchanger cooling, turn back to the high pressure section of synthetic compressor, the infiltration gas of second stage separatory membrane is after the 3rd gas-gas heat exchanger cooling, turn back to the low-pressure stage of synthetic compressor, second stage separatory membrane retain gas after the cooling of first gas-gas heat exchanger, enter ammonia recovering process.Wherein, according to practical situation, film can be divided into one-level or two-stage separatory membrane.Adopt flash trapping stage membrane process, the infiltration gas (being rich in hydrogen and ammonia) of separatory membrane turns back to the low-pressure stage of synthetic compressor; Adopt the second-order separation membrane process, the infiltration gas (being rich in hydrogen and ammonia) of first step separatory membrane turns back to the high pressure section of synthetic compressor, and the infiltration gas (being rich in hydrogen and ammonia) of second stage separatory membrane turns back to the low-pressure stage of synthetic compressor.Under the rate of recovery condition of same hydrogen and ammonia, two-stage separation membrane procedure can reduce the watt consumption of synthetic compressor.
For technique scheme, preferred embodiment is: in described ammonia recovering process, and the process of ammonia still process is: the gas phase entering ammonia still process rises to ammonia still process tower top, and liquid phase drops at the bottom of ammonia still; Rise to the gas phase of ammonia still process tower top, enter condenser and be cooled to liquefied ammonia.
For technique scheme, preferred embodiment is: the described liquefied ammonia being cooled acquisition by condenser, a part is back to the top of ammonia still as phegma through reflux pump, and another part is as liquefied ammonia Product recycling.Wherein, in condenser, the gas ammonia water cooling that is cooled is liquefied ammonia, and its ammonia density is greater than 99.5wt%;
For technique scheme, preferred embodiment is: the process that the described gas phase entering ammonia still process rises to ammonia still process tower top be by ammonia still bottom reboiler realize.
For technique scheme, preferred embodiment is: described reboiler adopts steam or high temperature heat conductive oil as thermal source.
For technique scheme, preferred embodiment is: also comprise cooling water circulation process, the water recycled from ammonia still reclaims after heat through the interchanger ammonia recovering process, then through the cooling of recirculated water cooler, finally by high-pressure pump, water is turned back to the recycle of ammonia absorber top.Wherein, the ammonia density of the water recycled from ammonia still is less than 200ppmw.
The present invention compared to existing technology tool has the following advantages:
1. the ammonia recovering process of traditional WATER-WASHING METHOD is placed in the downstream of membrane separating process, any abnormal operation of water washing process all can not impact membrane separating process, inherently ensure that the safety of membrane separating process, steady running.
2. membrane process long-term stability is run, and can ensure the recovery of more than 85% hydrogen recovery and more than 75% ammonia.
3. due to retain that tolerance only accounts for former synthetic ammonia periodic off-gases tolerance 20 ~ 40% after membrane sepn, the amount of ammonia only has original 20 ~ 30%, so the involved facility investment of ammonia recovering process, take up an area and reduce 60%; The energy consumption of ammonia absorber and ammonia still reduces 70 ~ 80% simultaneously, and running cost decreases 70 ~ 80%.
4. membrane process and ammonia recovering process can realize the recovery of more than 85% hydrogen recovery and nearly 100% ammonia.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of example 1 of the present invention;
Fig. 2 is the process flow diagram of example 2 of the present invention;
Wherein, 1. strainer; 2. first step interchanger; 3. second stage interchanger; 4. third stage interchanger; 5. well heater; 6. first step separatory membrane; 7. second stage separatory membrane; 21. ammonia absorbers; 22. high-pressure pump; 23. water recirculators; 24. interchanger; 25. tower bottom reboilers; 26. ammonia stills; 27. overhead condensers; 28. surge tanks; 29. reflux pumps.
Embodiment
Below in conjunction with accompanying drawing and embodiment, the present invention is described in further detail, the present invention of those of ordinary skill in the art's comprehend can be made, but do not limit the present invention in any way.Pressure described in literary composition is gauge pressure.
Embodiment 1
In the recovery synthetic ammonia periodic off-gases shown in Fig. 1 the method example 1 of hydrogen and ammonia process flow diagram in, the synthetic ammonia periodic off-gases discharged by synthesis system, its blowdown presssure is 13MPa, and temperature is 26 DEG C, and tolerance is 12000Nm3/hr, composed as follows:
| Component | H 2 | N 2 | CH 4 | Ar | NH 3 |
| Content %(V/V) | 64.98 | 28.09 | 2.11 | 2.13 | 2.69 |
First this periodic off-gases enters strainer 1, and removing air-flow possibility entrained solid particle and drop, the impurity being filtered out discharges from the bottom blow-down mouth of strainer 1.Gas after filtration is through first step interchanger 2, with second stage separatory membrane retain gas heat exchange, the temperature of gas is elevated to 41.8 DEG C, then through second stage interchanger 3, infiltration gas heat exchange with first step separatory membrane, is elevated to 47.5 DEG C by the temperature of gas, then through third stage interchanger 4, infiltration gas heat exchange with second stage separatory membrane, is elevated to 55 DEG C by the temperature of gas.Then enter well heater 5, gas temperature be elevated to 80 DEG C, well heater 5 thermal source be low-pressure steam.First the gas reached into film temperature enter first step separatory membrane 6, and the mould material of use is polyaramide, after first step separatory membrane is separated, obtain the first step and be separated membrane permeate gas, its pressure is 7.2MPa, and temperature is 80 DEG C, tolerance is 2854Nm3/hr, composed as follows:
| Component | H 2 | N 2 | CH 4 | Ar | NH 3 |
| Content %(V/V) | 92.24 | 3.68 | 0.18 | 0.58 | 3.32 |
After this gas and second stage interchanger 3 heat exchange, temperature drops to 55 DEG C, delivers to synthetic compressor high pressure section entrance.First step separatory membrane 6 be separated after retain gas, enter into second stage separatory membrane 7, the mould material of use is polyaramide, further recover hydrogen and ammonia.
After second stage separatory membrane 7 is separated, obtain the second stage and be separated membrane permeate gas, its pressure is 3.3MPa, and temperature is 80 DEG C, and tolerance is 4736Nm3/hr, composed as follows:
| Component | H 2 | N 2 | CH 4 | Ar | NH 3 |
| Content %(V/V) | 90.15 | 5.03 | 0.28 | 0.84 | 3.70 |
After this gas and third stage interchanger 4 heat exchange, temperature drops to 60 DEG C, delivers to synthetic compressor low-pressure stage entrance.Second stage separatory membrane 7 be separated after retain gas, its pressure is 12.8MPa, and temperature is 80 DEG C, and tolerance is 4410Nm3/hr, composed as follows:
| Component | H 2 | N 2 | CH 4 | Ar | NH 3 |
| Content %(V/V) | 20.30 | 68.65 | 5.33 | 4.53 | 1.19 |
After this gas and first step interchanger 2 heat exchange, temperature drops to 40 DEG C, delivers to next step ammonia recovering process.In membrane separating process, the rate of recovery of hydrogen is 88.52%, and the rate of recovery of ammonia is 83.73%, so follow-up ammonia recovering process load is the ammonia of in former synthetic ammonia periodic off-gases 16.27%.
First the gas come from membrane sepn part enter bottom ammonia absorber 21, and upruss contacts with water.Gas is after ammonia absorber washing removing ammonia, and deliver to fuel gas system, its pressure is 12.5MPa, and temperature is 45 DEG C, and tolerance is 4360Nm3/hr, composed as follows:
| Component | H 2 | N 2 | CH 4 | Ar | NH 3 |
| Content %(V/V) | 20.53 | 20.53 | 20.53 | 20.53 | <10ppmv |
The ammonia soln obtained bottom ammonia absorber, the concentration of ammonia is 10wt%, and flow is 399.05kg/hr.Through interchanger 24, by ammoniacal liquor pre-heating temperature elevation to 180 DEG C, then enter ammonia still 26.The working pressure of ammonia still is 2.0MPa, and the service temperature of tower bottom reboiler is 216 DEG C, and heating medium is steam, and the service temperature of overhead condenser 27 is 40 DEG C, and heat-eliminating medium is recirculated water.The liquefied ammonia that tower top obtains, after surge tank 28, then through reflux pump 29 will wherein a part be as trim the top of column liquid, another part is as liquefied ammonia product, and the concentration of liquefied ammonia is 99.8wt%, and flow is 39.6kg/hr.Be less than the aqueous solution of 200ppmw bottom ammonia still to ammonia density, temperature is 216.7 DEG C, and a part of liquid is after tower bottom reboiler 25 heating and gasifying, enter ammonia still 26, remaining liquid phase, flow is 358.57kg/hr, reclaims heat through interchanger 24, fall within the range of 61.77 DEG C, again through water recirculator 23, reduce the temperature to 40 DEG C, the pressure of the aqueous solution is elevated to 12.6MPa by high-pressure pump 22, turn back to ammonia absorber, recycle.
Embodiment 2
In the recovery synthetic ammonia periodic off-gases shown in Fig. 2 the method example 2 of hydrogen and ammonia process flow diagram in, the synthetic ammonia periodic off-gases discharged by synthesis system, its blowdown presssure is 12.3MPa, and temperature is 25 DEG C, and tolerance is 8000Nm3/hr, composed as follows:
| Component | H 2 | N 2 | CH 4 | Ar | NH 3 |
| Content %(V/V) | 63.00 | 21.84 | 8.10 | 3.55 | 3.50 |
First this periodic off-gases enters strainer 1, and removing air-flow possibility entrained solid particle and drop, the impurity being filtered out discharges from the bottom blow-down mouth of strainer 1.Gas after filtration is through first step interchanger 2, with membrane sepn retain gas heat exchange, the temperature of gas is elevated to 37.68 DEG C, then through second stage interchanger 3, infiltration gas heat exchange with membrane sepn, is elevated to 46.3 DEG C by the temperature of gas, then enters well heater 4, gas temperature is elevated to 70 DEG C, well heater 4 thermal source be low-pressure steam.First the gas reached into film temperature enter membrane separation apparatus 5, and the mould material used in membrane separation apparatus is polyaramide, and after membrane sepn, obtain membrane permeate gas, its pressure is 2.6MPa, and temperature is 70 DEG C, and tolerance is 4969Nm3/hr, composed as follows:
| Component | H 2 | N 2 | CH 4 | Ar | NH 3 |
| Content %(V/V) | 91.46 | 2.61 | 0.62 | 0.89 | 4.42 |
After this gas and second stage interchanger 3 heat exchange, temperature drops to 55 DEG C, delivers to synthetic compressor low-pressure stage entrance.Retain gas after membrane sepn, its pressure is 12.15MPa, and temperature is 70 DEG C, and tolerance is 3031Nm3/hr, composed as follows:
| Component | H 2 | N 2 | CH 4 | Ar | NH 3 |
| Content %(V/V) | 16.37 | 53.37 | 20.36 | 7.91 | 1.99 |
After this gas and first step interchanger 2 heat exchange, temperature drops to 40 DEG C, delivers to next step ammonia recovering process.
In film removal process, the rate of recovery of hydrogen is 90.16%, and the rate of recovery of ammonia is 78.48%, so follow-up ammonia recovering process load is the ammonia of in former synthetic ammonia periodic off-gases 21.52%.
Gas from membrane sepn part is first from entering bottom ammonia absorber 21, and upruss contacts with water.Gas is after ammonia absorber washing removing ammonia, and deliver to fuel gas system, its pressure is 11.9MPa, and temperature is 47 DEG C, and tolerance is 2973Nm3/hr, composed as follows:
| Component | H 2 | N 2 | CH 4 | Ar | NH 3 |
| Content %(V/V) | 16.69 | 54.41 | 20.76 | 8.06 | <10ppmv |
The ammonia soln obtained bottom ammonia absorber, the concentration of ammonia is 12wt%, and flow is 381.16kg/hr.Through interchanger 24, by ammoniacal liquor pre-heating temperature elevation to 180 DEG C, then enter ammonia still 26.The working pressure of ammonia still is 1.85MPa, and the service temperature of tower bottom reboiler is 212 DEG C, and heating medium is steam, and the service temperature of overhead condenser 27 is 40 DEG C, and heat-eliminating medium is recirculated water.The liquefied ammonia that tower top obtains, after surge tank 28, then through reflux pump 29 will wherein a part be as trim the top of column liquid, another part is as liquefied ammonia product, and the concentration of liquefied ammonia is 99.8wt%, and flow is 45.39kg/hr.Be less than the aqueous solution of 200ppmw bottom ammonia still to ammonia density, temperature is 212 DEG C, and a part of liquid, after tower bottom reboiler 25 heating and gasifying, enters ammonia still 26, remaining liquid phase, and flow is 334.5kg/hr.The aqueous solution reclaims heat through interchanger 24, falls within the range of 57.06 DEG C, then through water recirculator 23, reduces the temperature to 40 DEG C, and the pressure of the aqueous solution is elevated to 12.1MPa by high-pressure pump 22, turns back to ammonia absorber, recycle.
Energy consumption and the running cost of ammonia recovering process decrease 70 ~ 80%.It is embodied in: the consumption of the absorption liquid in ammonia recovering process decreases 70 ~ 80%, the heat exhaustion of reboiler decreases 70 ~ 80%, the thermal exchange of other interchanger decreases 70 ~ 80%, so the power consumption of pump, the steam of reboiler or the consumption of heating thermal oil, the consumption of recirculated cooling water all consequently reduce 70 ~ 80%.
Claims (1)
1. the method for recover hydrogen and ammonia from synthetic ammonia periodic off-gases, is characterized in that: comprise preprocessing process, membrane separating process and ammonia recovering process;
Described preprocessing process: synthetic ammonia periodic off-gases first through strainer removing solid particulate and drop, then after gas-gas heat exchanger progressively heats up, is warmed up to 45 ~ 90 DEG C by well heater;
Described membrane separating process: through the gas of preprocessing process process, after separatory membrane process, the gas of the per-meate side enrichment of separatory membrane, after the gas-gas heat exchanger cooling in preprocessing process, is reclaimed by synthetic compressor; The gas retaining lateral enrichment of separatory membrane, after the gas-gas heat exchanger cooling in preprocessing process, enters ammonia recovering process; Described separation membrane material is polyaramide;
Described ammonia recovering process: the synthetic ammonia periodic off-gases after membrane separating process process, enters from the bottom of ammonia absorber, upruss, after ammonia absorber washing removing ammonia, delivers to fuel gas system; By the ammonia soln obtained bottom ammonia absorber, after interchanger is warmed up to 150 ~ 190 DEG C, enter ammonia still process; Obtain liquefied ammonia product at the tower top of ammonia still, the aqueous solution obtained at the bottom of tower returns ammonia absorber recycle.
2. the method for recover hydrogen and ammonia from synthetic ammonia periodic off-gases according to claim 1, is characterized in that: the gas-gas heat exchanger in described preprocessing process is 3 series connection; The separatory membrane of described membrane separating process is 2 series connection; The infiltration gas of first step separatory membrane is after second gas-gas heat exchanger cooling, turn back to the high pressure section of synthetic compressor, the infiltration gas of second stage separatory membrane is after the 3rd gas-gas heat exchanger cooling, turn back to the low-pressure stage of synthetic compressor, second stage separatory membrane retain gas after the cooling of first gas-gas heat exchanger, enter ammonia recovering process.
3. the method for recover hydrogen and ammonia from synthetic ammonia periodic off-gases according to claim 1, it is characterized in that: in described ammonia recovering process, the process of ammonia still process is: the gas phase entering ammonia still process rises to ammonia still process tower top, and liquid phase drops at the bottom of ammonia still; Rise to the gas phase of ammonia still process tower top, enter condenser and be cooled to liquefied ammonia.
4. the method for recover hydrogen and ammonia from synthetic ammonia periodic off-gases according to claim 3, it is characterized in that: cooled the liquefied ammonia obtained by condenser, a part is back to the top of ammonia still as phegma through reflux pump, and another part is as liquefied ammonia Product recycling.
5. the method for recover hydrogen and ammonia from synthetic ammonia periodic off-gases according to claim 3, is characterized in that: the process that the described gas phase entering ammonia still process rises to ammonia still process tower top be by ammonia still bottom reboiler realize.
6. the method for recover hydrogen and ammonia from synthetic ammonia periodic off-gases according to claim 1, it is characterized in that: also comprise cooling water circulation process, the water recycled from ammonia absorber reclaims after heat through the interchanger ammonia recovering process, again through the cooling of recirculated water cooler, finally by high-pressure pump, water is turned back to the recycle of ammonia absorber top.
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| CN102515099A (en) * | 2011-12-07 | 2012-06-27 | 天邦膜技术国家工程研究中心有限责任公司 | Membrane separation method and device for recycling hydrogen from purge gas of synthetic ammonia liquid ammonia storage tank |
| CN102530990A (en) * | 2011-12-22 | 2012-07-04 | 天邦膜技术国家工程研究中心有限责任公司 | Method for recovering hydrogen and ammonia from synthetic ammonia purge gas by membrane separation-rectification integrated technology and device |
| CN203295210U (en) * | 2013-02-07 | 2013-11-20 | 上海兄弟微电子技术有限公司 | Ammonia gas recovering system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US5538536A (en) * | 1994-09-12 | 1996-07-23 | L'air Liquide, Societe Anonyme Pour L'etude Et L'eploitation Des Procedes Georges Claude | Process and apparatus for separation of a gaseous mixture by successive membranes of different selectivities |
| CN101590364A (en) * | 2009-07-07 | 2009-12-02 | 贵州赤天化股份有限公司 | Gas and synthetic ammonia purge and basin gas are carried out method and the device that hydrogen reclaims |
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Denomination of invention: Method for recovering hydrogen and ammonia from synthetic ammonia exhaust gas Effective date of registration: 20230927 Granted publication date: 20150408 Pledgee: China CITIC Bank Co.,Ltd. Dalian Branch Pledgor: DALIAN EUROFILM INDUSTRIAL Ltd. Registration number: Y2023980059270 |