CN103663367A - 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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- CN103663367A CN103663367A CN201310699052.8A CN201310699052A CN103663367A CN 103663367 A CN103663367 A CN 103663367A CN 201310699052 A CN201310699052 A CN 201310699052A CN 103663367 A CN103663367 A CN 103663367A
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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 relief gas reclaims, related in particular to a kind of from synthetic ammonia relief gas the method for recover hydrogen and ammonia.
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 generally obtains 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 supplementary virgin gas.Because synthetic ammonia feedstock nitrogen and hydrogen all contain a certain amount of inert component argon gas and methane, these inert components are constantly accumulation in working cycle, not only consume loop compression merit, also can make the useful volume of synthetic tower 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 relief gas.Be about～300Nm of discharge tolerance
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.
Mostly adopt at present membrane separation technique to fold into back and forth hydrogen and ammonia in ammonia relief gas.Because current mould material is to the non-constant of the tolerance of ammonia, so high pressure is speeded, venting 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 of ammonia in gas phase below 0.02%, and then enter membrane separation apparatus and reclaim the hydrogen speed in venting, the hydrogen that the infiltration gas of film is 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, as fuel, uses.Aforesaid method is very strict to the operational requirement of ammonia absorber, can not occur ammonia concentration over-standard in gas phase, more will definitely avoid occurring the generation of entrainment and Concerning Flooding Phenomenon, otherwise can cause the expendable damage of downstream separation film.In actual application process, because ammonia absorber operation goes wrong, the example that causes 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 relief gas; It is a kind of for realizing described synthetic ammonia relief gas hydrogen and the device of ammonia that another object is to provide.
The present invention adopts and can withstand long term exposure ammonia phase concentration to be less than 6%(V/V) the film of resistance to ammonia process synthetic ammonia relief gas, reclaim hydrogen and most of ammonia wherein, then adopt the method for washing and ammonia still process, after reclamation film separation, hold back the ammonia containing in gas, become liquefied ammonia product.Of the present invention from synthetic ammonia relief gas the method for recover hydrogen and ammonia, its key step comprises preprocessing process, membrane sepn process and ammonia recovering process;
Described preprocessing process: first synthetic ammonia relief gas removes solid particulate and drop through strainer, then after gas-gas heat exchanger progressively heats up, is warmed up to 45～90 ℃ by well heater; Wherein, 1. described process strainer is removed solid particulate and drop, is conducive to prevent that mechanical impurity from entering separatory membrane, is conducive to guarantee separation performance and the work-ing life of film; 2. pass through continuously gas-gas heat exchanger, not only the temperature of ammonia relief gas is raise, can also reclaim separated membrane permeate gas and the heat of holding back gas.3. the well heater in the preprocessing process described in, its thermal source can be steam, deep fat, electricity or other high-temperature medium; Use well heater to improve gas and enter film temperature, guaranteed that gas departs from its dew-point temperature more than 5～20 ℃, to have prevented that liquid from condensing on film, causes the damage of film.
Described membrane sepn process: the gas of processing through preprocessing process, after separatory membrane is processed, the gas of the per-meate side enrichment of separatory membrane, after the gas-gas heat exchanger cooling in preprocessing process, reclaims by synthetic compressor; The gas of holding back 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 is that hydrogen and ammonia all preferentially see through, and in the per-meate side enrichment of separatory membrane, then delivers to synthetic compressor entrance, turns back to ammonia synthesis system, realizes the recovery of ammonia more than more than 85% hydrogen and 75%.Separatory membrane hold back the gas that side is enrich methane, argon gas, nitrogen and residue ammonia.2. after membrane sepn process, ammonia more than more than 85% hydrogen and 75% is recycled utilization, but holding back in gas of separatory membrane still contains a certain amount of ammonia, and these gases are all used as fuel gas conventionally.But due to the existence of ammonia, can cause the content overproof of NOx in the gas after burning, also cause the loss of ammonia simultaneously.So the present invention adopts ammonia to absorb and the way of ammonia still process is held back ammonia in gas by film and reclaimed with the form of liquefied ammonia, thereby realizes the recovery of synthesizing ammonia nearly 100% in ammonia relief gas.
Described ammonia recovering process: the synthetic ammonia relief gas after membrane sepn process is processed, from the bottom of ammonia absorber, enter, upruss, after ammonia absorber is washed and removed ammonia, is delivered to fuel gas system; The ammonia soln being obtained by ammonia absorber bottom enters ammonia still and processes after interchanger is warmed up to 150～190 ℃.Wherein, in the ammonia soln that ammonia absorber bottom obtains, the concentration of ammonia is 5～20wt%.In ammonia still, realize the separated of ammonia and water, at tower top, obtain purity and be greater than 99.5wt% liquefied ammonia product, at the bottom of tower, obtain the aqueous solution that ammonia concentration is less than 200ppmw, then by high-pressure pump, return it to ammonia absorber recycle.
For technique scheme, in the preferred case, described separation membrane material is polyaramide.Because the NH3 content of speeding in venting 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 polyaramide material 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 sepn 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 hold back 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 of separatory membrane (being rich in hydrogen and ammonia) turns back to the low-pressure stage of synthetic compressor; Adopt the second-order separation membrane process, the infiltration gas of first step separatory membrane (being rich in hydrogen and ammonia) turns back to the high pressure section of synthetic compressor, and the infiltration gas of second stage separatory membrane (being rich in hydrogen and ammonia) turns back to the low-pressure stage of synthetic compressor.Under the rate of recovery condition of same hydrogen and ammonia, two-stage separatory membrane process can reduce the watt consumption of synthetic compressor.
For technique scheme, preferred embodiment is: in described ammonia recovering process, the process that ammonia still is processed is: the gas phase that enters ammonia still processing rises to ammonia still process tower top, at the bottom of liquid phase drops to 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 by the cooling acquisition of condenser, and the top that a part is back to ammonia still through reflux pump is as phegma, and another part reclaims as liquefied ammonia product.Wherein, in condenser, the gas ammonia water cooling that is cooled is liquefied ammonia, and its ammonia concentration is greater than 99.5wt%;
For technique scheme, preferred embodiment is: the process that the described gas phase that enters ammonia still processing rises to ammonia still process tower top is to realize by the reboiler of ammonia still bottom.
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 recycling from ammonia still, after interchanger ammonia recovering process reclaims heat, then through the cooling of recirculated water cooler, finally turns back to the recycle of ammonia absorber top by high-pressure pump by water.The ammonia concentration of the water wherein, recycling 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 to the downstream of membrane sepn process, any abnormal operation of water washing process can not impact membrane sepn process, from having guaranteed in essence safety, the steady running of membrane sepn process.
2. membrane process operation steady in a long-term, can guarantee the recovery of 85% above hydrogen recovery and 75% above ammonia.
3. because the tolerance of holding back after membrane sepn only accounts for 20～40% of former synthetic ammonia relief gas tolerance, it is original 20～30% that the amount of ammonia only has, so the related facility investment of ammonia recovering process, take up an area and reduced by 60%; Simultaneously the Energy Intensity Reduction of ammonia absorber and ammonia still 70～80%, running cost has reduced 70～80%.
4. membrane process and ammonia recovering process can realize the recovery of 85% above hydrogen recovery and nearly 100% ammonia.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of the inventive example 1;
Fig. 2 is the process flow diagram of the inventive example 2;
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, can makes the present invention of those of ordinary skill in the art's comprehend, but not limit the present invention in any way.Pressure described in literary composition is gauge pressure.
Embodiment 1
In the synthetic ammonia relief gas of the recovery shown in Fig. 1 in the process flow diagram of the method example 1 of hydrogen and ammonia, the synthetic ammonia relief gas being discharged by synthesis system, its blowdown presssure is 13MPa, and temperature is 26 ℃, 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 venting of speeding enters strainer 1, removes air-flow possibility entrained solid particle and drop, and the impurity that is filtered is out from the bottom blow-down mouth discharge of strainer 1.Gas after filtration is through first step interchanger 2, with second stage separatory membrane hold back gas heat exchange, the temperature of gas is elevated to 41.8 ℃, then through second stage interchanger 3, infiltration gas heat exchange with first step separatory membrane, is elevated to 47.5 ℃ by the temperature of gas, then passes through third stage interchanger 4, infiltration gas heat exchange with second stage separatory membrane, is elevated to 55 ℃ by the temperature of gas.Then enter well heater 5, gas temperature is elevated to 80 ℃, 5 thermal source of well heater is low-pressure steam.Reach into the gas of film temperature and first enter first step separatory membrane 6, the mould material of use is polyaramide, after the separation of first step separatory membrane, obtain the separated membrane permeate gas of the first step, its pressure is 7.2MPa, and temperature is 80 ℃, 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 3 heat exchange of second stage interchanger, temperature drops to 55 ℃, delivers to synthetic compressor high pressure section entrance.After 6 separation of first step separatory membrane, hold back gas, enter into second stage separatory membrane 7, the mould material of use is polyaramide, further recover hydrogen and ammonia.
After 7 separation of second stage separatory membrane, obtain the separated membrane permeate gas in the second stage, its pressure is 3.3MPa, and temperature is 80 ℃, 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 4 heat exchange of third stage interchanger, temperature drops to 60 ℃, delivers to synthetic compressor low-pressure stage entrance.After 7 separation of second stage separatory membrane, hold back gas, its pressure is 12.8MPa, and temperature is 80 ℃, 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 2 heat exchange of first step interchanger, temperature drops to 40 ℃, delivers to next step ammonia recovering process.In membrane sepn 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 16.27% ammonia in former synthetic ammonia relief gas.
First the gas partly coming from membrane sepn enter ammonia absorber 21 bottoms, and upruss contacts with water.Gas, after ammonia is removed in ammonia absorber washing, is delivered to fuel gas system, and its pressure is 12.5MPa, and temperature is 45 ℃, 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 that ammonia absorber bottom obtains, the concentration of ammonia is 10wt%, flow is 399.05kg/hr.Through interchanger 24, by ammoniacal liquor pre-heating temperature elevation to 180 ℃, then enter ammonia still 26.The working pressure of ammonia still is 2.0MPa, and the service temperature of tower bottom reboiler is 216 ℃, and heating medium is steam, and the service temperature of overhead condenser 27 is 40 ℃, and heat-eliminating medium is recirculated water.The liquefied ammonia that tower top obtains, after surge tank 28, wherein a part is as trim the top of column liquid through reflux pump 29, and another part is as liquefied ammonia product, and the concentration of liquefied ammonia is 99.8wt%, and flow is 39.6kg/hr.Ammonia still bottom is less than the aqueous solution of 200ppmw to ammonia concentration, temperature is 216.7 ℃, and a part of liquid is after tower bottom reboiler 25 heating and gasifyings, enter ammonia still 26, remaining liquid phase, flow is 358.57kg/hr, through interchanger 24, reclaims heat, fall within the range of 61.77 ℃, pass through water recirculator 23 again, reduce the temperature to 40 ℃, high-pressure pump 22 is elevated to 12.6MPa by the pressure of the aqueous solution, turn back to ammonia absorber, recycle.
In the synthetic ammonia relief gas of the recovery shown in Fig. 2 in the process flow diagram of the method example 2 of hydrogen and ammonia, the synthetic ammonia relief gas being discharged by synthesis system, its blowdown presssure is 12.3MPa, and temperature is 25 ℃, 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 venting of speeding enters strainer 1, removes air-flow possibility entrained solid particle and drop, and the impurity that is filtered is out from the bottom blow-down mouth discharge of strainer 1.Gas after filtration is through first step interchanger 2, with membrane sepn hold back gas heat exchange, the temperature of gas is elevated to 37.68 ℃, then through second stage interchanger 3, infiltration gas heat exchange with membrane sepn, is elevated to 46.3 ℃ by the temperature of gas, then enters well heater 4, gas temperature is elevated to 70 ℃, and 4 thermal source of well heater is low-pressure steam.Reach into the gas of film temperature and first enter membrane separation apparatus 5, the mould material using in membrane separation apparatus is polyaramide, after membrane sepn, obtains membrane permeate gas, and its pressure is 2.6MPa, and temperature is 70 ℃, 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 3 heat exchange of second stage interchanger, temperature drops to 55 ℃, delivers to synthetic compressor low-pressure stage entrance.After membrane sepn, hold back gas, its pressure is 12.15MPa, and temperature is 70 ℃, 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 2 heat exchange of first step interchanger, temperature drops to 40 ℃, 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 21.52% ammonia in former synthetic ammonia relief gas.
The gas partly coming from membrane sepn is first from entering ammonia absorber 21 bottoms, and upruss contacts with water.Gas, after ammonia is removed in ammonia absorber washing, is delivered to fuel gas system, and its pressure is 11.9MPa, and temperature is 47 ℃, 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 that ammonia absorber bottom obtains, the concentration of ammonia is 12wt%, flow is 381.16kg/hr.Through interchanger 24, by ammoniacal liquor pre-heating temperature elevation to 180 ℃, then enter ammonia still 26.The working pressure of ammonia still is 1.85MPa, and the service temperature of tower bottom reboiler is 212 ℃, and heating medium is steam, and the service temperature of overhead condenser 27 is 40 ℃, and heat-eliminating medium is recirculated water.The liquefied ammonia that tower top obtains, after surge tank 28, wherein a part is as trim the top of column liquid through reflux pump 29, and another part is as liquefied ammonia product, and the concentration of liquefied ammonia is 99.8wt%, and flow is 45.39kg/hr.Ammonia still bottom is less than the aqueous solution of 200ppmw to ammonia concentration, temperature is 212 ℃, and a part of liquid, after tower bottom reboiler 25 heating and gasifyings, 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 ℃, then passes through water recirculator 23, reduces the temperature to 40 ℃, and high-pressure pump 22 is elevated to 12.1MPa by the pressure of the aqueous solution, turns back to ammonia absorber, recycle.
Energy consumption and the running cost of ammonia recovering process have reduced 70～80%.It is embodied in: the consumption of the absorption liquid in ammonia recovering process has reduced 70～80%, the heat exhaustion of reboiler has also reduced 70～80%, the thermal exchange of other interchanger has also reduced 70～80%, thus the power consumption of pump, the steam of reboiler or heating with the consumption of thermal oil, the consumption of recirculated cooling water has all reduced 70～80% accordingly.
Claims (7)
1. a method for recover hydrogen and ammonia from synthetic ammonia relief gas, is characterized in that: comprise preprocessing process, membrane sepn process and ammonia recovering process;
Described preprocessing process: first synthetic ammonia relief gas removes solid particulate and drop through strainer, then after gas-gas heat exchanger progressively heats up, is warmed up to 45～90 ℃ by well heater;
Described membrane sepn process: the gas of processing through preprocessing process, after separatory membrane is processed, the gas of the per-meate side enrichment of separatory membrane, after the gas-gas heat exchanger cooling in preprocessing process, reclaims by synthetic compressor; The gas of holding back lateral enrichment of separatory membrane, after the gas-gas heat exchanger cooling in preprocessing process, enters ammonia recovering process;
Described ammonia recovering process: the synthetic ammonia relief gas after membrane sepn process is processed, from the bottom of ammonia absorber, enter, upruss, after ammonia absorber is washed and removed ammonia, is delivered to fuel gas system; The ammonia soln being obtained by ammonia absorber bottom enters ammonia still and processes after interchanger is warmed up to 150～190 ℃; Tower top at ammonia still obtains liquefied ammonia product, and the aqueous solution obtaining at the bottom of tower returns to ammonia absorber recycle.
According to claim 1 from synthetic ammonia relief gas the method for recover hydrogen and ammonia, it is characterized in that: described separation membrane material is polyaramide.
According to claim 1 from synthetic ammonia relief gas the method for recover hydrogen and ammonia, it is characterized in that: the gas-gas heat exchanger in described preprocessing process is 3 series connection; The separatory membrane of described membrane sepn 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 hold back gas after the cooling of first gas-gas heat exchanger, enter ammonia recovering process.
According to claim 1 from synthetic ammonia relief gas the method for recover hydrogen and ammonia, it is characterized in that: in described ammonia recovering process, the process that ammonia still is processed is: the gas phase that enters ammonia still processing rises to ammonia still process tower top, at the bottom of liquid phase drops to ammonia still; Rise to the gas phase of ammonia still process tower top, enter condenser and be cooled to liquefied ammonia.
According to claim 4 from synthetic ammonia relief gas the method for recover hydrogen and ammonia, it is characterized in that: the described liquefied ammonia by the cooling acquisition of condenser, the top that a part is back to ammonia still through reflux pump is as phegma, and another part reclaims as liquefied ammonia product.
According to claim 4 from synthetic ammonia relief gas the method for recover hydrogen and ammonia, it is characterized in that: described to enter the process that gas phase that ammonia still processes rises to ammonia still process tower top be to realize by the reboiler of ammonia still bottom.
According to claim 1 from synthetic ammonia relief gas the method for recover hydrogen and ammonia, it is characterized in that: also comprise cooling water circulation process, the water recycling from ammonia absorber is after the interchanger ammonia recovering process reclaims heat, through the cooling of recirculated water cooler, finally by high-pressure pump, water is turned back to the recycle of ammonia absorber top again.
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| 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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| 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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- 2013-12-18 CN CN201310699052.8A patent/CN103663367B/en active Active
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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 |
| 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 |
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| 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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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 |