CN1552505A - Adsorption stripping method for removing ethene and carbon dioxide from mixed gas - Google Patents
Adsorption stripping method for removing ethene and carbon dioxide from mixed gas Download PDFInfo
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- CN1552505A CN1552505A CNA031351271A CN03135127A CN1552505A CN 1552505 A CN1552505 A CN 1552505A CN A031351271 A CNA031351271 A CN A031351271A CN 03135127 A CN03135127 A CN 03135127A CN 1552505 A CN1552505 A CN 1552505A
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Abstract
An adsorptive separation method for removing ethylene and CO2 from the gas mixture features that in a pressure-varying adsorption system composed of at least two adsorption beds filled by adsorbent chosen from activated carbon, aluminium oxide, silica gel and molecular sieve, easy cycle of adsorption bed includes sequentially such steps as adsorption and at least one lowering of pressure, reversely releasing pressure, vacuumizing or flushing, or at least one increasing of pressure.
Description
Technical field
The present invention relates to the method for divided gas flow.Particularly adopt transformation absorption from mist, to remove the method for ethene, carbon dioxide.
Background technology
From mist, the method that particularly removes ethene in the modified atmosphere fresh-keeping storage mist mainly is to adopt catalytic oxidation at present, catalytic oxidation is to utilize precious metal oxidation catalyst at high temperature the ethylene catalytic oxidation in the nitrogen (burning) to be become carbon dioxide and water, and the concentration that reduces ethene in the modified atmosphere fresh-keeping storage gas is to guarantee the normal operation of modified atmosphere fresh-keeping storage.This method is that the waste gas of modified atmosphere fresh-keeping storage is become carbon dioxide and water by oxidation catalyst with the ethylene catalytic oxidation in the nitrogen (burning) under～200 ℃ or higher temperature, purifies that ethylene contents can reach the level less than 10ppm in the gas of back.Since this method need the waste gas with modified atmosphere fresh-keeping storage all be heated to～200 ℃ or higher, be cooled to room temperature again after removing ethene, so energy consumption is bigger, operating cost is higher, and requires the sulfide content in the waste gas must be lower than 1ppm.This method can not remove carbon dioxide when removing ethene, also must adopt other method to remove carbon dioxide for modified atmosphere fresh-keeping storage gas.In addition, also have in packaging bag, or place activated carbon in the modified atmosphere fresh-keeping storage, the ethene in the absorption atmosphere such as silica, potassium permanganate and the method for carbon dioxide.This method can't be regenerated owing to the disposable use of adsorbent, so the cost height, only limits to usually use in small-sized packing.
Summary of the invention
In view of above-mentioned, the object of the present invention is to provide a kind ofly can from mist, remove ethene, carbon dioxide, purifying rate height, the adsorption method of separation that from mist, removes ethene, carbon dioxide that cost is low simultaneously.
The ethene that from mist, removes of the present invention, the adsorption method of separation of carbon dioxide (referring to accompanying drawing), in the pressure swing adsorption system of the circular flow of at least two adsorbent beds that are filled with adsorbent, mist is sent into adsorbent bed, each circulation of adsorbent bed has the absorption of experience successively, or all pressure drops are arranged at least once, the reverse pressure of putting, find time or wash, or all voltage rises are arranged at least once, the step of boosting, at adsorption step adsorbents adsorb removing impurities gas and be trapped in the adsorbent bed, obtain purified gas and discharge adsorbent bed, in the reverse pressure of putting, find time or rinsing step adsorbent desorption and regeneration and impurity gas discharged adsorbent bed, above-mentioned adsorbent is an active carbon, aluminium oxide, silica gel, at least a in the molecular sieve.
The absolute pressure of above-mentioned adsorption step can be 0.10～2.0MPa, and the absolute pressure of evacuation step is 0.007～0.05MPa, and the absolute pressure of rinsing step is 0.12～0.6MPa.
Above-mentioned mist can be the modified atmosphere fresh-keeping storage combustion gas, and when above-mentioned adsorbent was aluminium oxide and active carbon, the absolute pressure of adsorption step was 0.10～0.6MPa.
The flushing gas of above-mentioned rinsing step can be at least a in Purge gas, air, nitrogen, the adsorbent bed purified gas of discharging.
Method of the present invention adopts adsorbent that ethene in the mist that contains ethene or ethene and carbon dioxide and carbon dioxide are carried out adsorbing separation and removes the purified gas of acquisition.When gaseous mixture was the waste gas of modified atmosphere fresh-keeping storage, the purified gas of acquisition can directly return modified atmosphere fresh-keeping storage and recycle.
The activated carbon of sorbent that the present invention selects for use, aluminium oxide, silica gel, molecular sieve all have abundant microporous structure and bigger adsorption surface area, therefore ethene in the gaseous mixture and carbon dioxide had adsorptive selectivity, can be from gaseous mixture ethylene adsorption or and carbon dioxide and ethene, and only adsorb less nitrogen.
The adsorbing separation of the inventive method has bigger adsorption capacity based on adsorbent under higher absolute pressure to ethene and carbon dioxide, ethene and carbon dioxide are attracted on the adsorbent, from adsorbent bed outlet obtain low ethene and carbon dioxide content purified gas this be commonly called adsorption step.In adsorbent reactivation, by finding time or rinsing step reduces the dividing potential drop of ethene and carbon dioxide in the adsorbent bed, this moment, adsorbent reduced ethene and carbon dioxide adsorption capacity, ethene and carbon dioxide desorb and take adsorbent bed out of by exhaust and purge gas from adsorbent, adsorbent is restored to the absorption property of ethene and carbon dioxide, prepares to enter next adsorption step.
Pressure swing adsorption technique of the present invention needs two or more adsorbent beds at least, forms a continuous movement system, and treating capacity is big more, and ethene, carbon dioxide content are high more, and the adsorbent bed that then needs is many more.Each adsorbent bed experiences following steps successively in once circulating:
(1) absorption
With gaseous mixture from bottom to top send into absorption absolute pressure in 0.10～2.0MPa scope, be preferably on the adsorbent bed of 0.10～0.5MPa scope and adsorb, adsorbent in adsorbent bed adsorbs ethene and carbon dioxide, and purified gas is discharged from the adsorbent bed top.When the forward position of adsorption zone is moved upwards up to the certain position of adsorbent bed, ethene, carbon dioxide reach normal concentration in exit gas after, to end to enter unstripped gas, stop absorption, another adsorbent bed that this moment, unstripped gas entered after regenerating adsorbs.
All pressure drops
Comprise the equal pressure drop of one or many, when the absorption absolute pressure is lower than 0.2MPa, can not adopt equal voltage drop step.Opening controlling valve after adsorption step is finished, utilize pressure-equalizing passageway make adsorbent bed with find time or rinsing step after adsorbent bed be connected, the gas of the higher adsorbent bed of absolute pressure flows into the lower adsorbent bed of absolute pressure, makes adsorbent bed absolute pressure balance.All the main effect of pressure drop is the absolute pressure that reduces adsorbent bed, and adsorbent bed is included the absolute pressure that adsorbent bed that ethene and carbon dioxide less gas be recycled to equal voltage rise improves equal voltage rise adsorbent bed simultaneously.
(3) the reverse pressure of putting
When the absorption absolute pressure is higher than 0.1MPa, make adsorbent bed reverse pressure of putting under the absorption absolute pressure, gas is emitted from the adsorbent bed bottom reach atmospheric pressure state.Reverse main effect of putting pressure is to reduce the absolute pressure of adsorbent bed to make ethene, the carbon dioxide desorb that partly is adsorbed on the adsorbent.
(4) find time or wash
With vavuum pump adsorbent bed is found time to reduce adsorbent bed absolute pressure to 0.007～0.05MPa, ethene, carbon dioxide are desorbed from adsorbent, adsorbent obtains regeneration so that recycle.
Developing technique utilizes at least a gas in a part of purified gas that another absorption adsorbent bed discharges, air, nitrogen, the purified gas as purge gas, the purge gas of 0.12～0.6MPa absolute pressure is from top to bottom passed through adsorbent bed, make the ethene, the carbon dioxide desorb that are adsorbed on the adsorbent, adsorbent is reproduced.
All voltage rises
Comprise the equal voltage rise of one or many, when the absorption absolute pressure is lower than 0.2MPa, can not adopt equal voltage rise step.Find time or rinsing step finish after opening controlling valve, the adsorbent bed after utilizing pipeline to make adsorbent bed and adsorption step is finished is connected, the gas of the higher adsorbent bed of absolute pressure flows into the low adsorbent bed of absolute pressure, makes adsorbent bed absolute pressure balance.
(6) boost
With purified gas adsorbent bed is boosted to the absorption absolute pressure.
The circular flow each time of each adsorbent bed can be experienced absorption successively, reversely puts pressure, the step of finding time, boost; Also can experience absorption successively, reversely put pressure, the step of washing, boost; Can experience absorption, at least once all pressure drops successively, reversely put pressures, find time, at least once equal voltage rise, the step of boosting; Can also experience absorption, at least once all pressure drops, reverse pressures, flushing, at least once equal voltage rise, the step of boosting of putting successively.Each adsorbent bed all will experience identical step, just diverge mutually on the sequential, carry out continuously to guarantee separation process.Promptly for adsorbent bed, circular flow each time has the absorption and the two kinds of running statuses of regenerating, and is in adsorbed state when adsorption step, is in reproduced state when all the other steps.End when a part of adsorbent bed is in absorption, then another partly adsorbent bed to be in absorption initial, thereby system is moved continuously.
The present invention can carry out compared with prior art at normal temperatures, need not heat, and adsorbent can regeneration cycle use, and it is low therefore to have energy consumption, the advantage that operating cost is low.The present invention does not have particular restriction to oxygen content in the gaseous mixture and sulfide content.The inventive method adopts inhales the adsorbent of carbon adsorptive selectivity excellence to ethene, titanium dioxide, when in absorption, find time or rinsing step when adopting suitable absolute pressure, ethene, titanium dioxide are inhaled the removal efficiency height of carbon.Particularly when being used to purify modified atmosphere fresh-keeping storage waste gas, the ethylene contents of purified gas can be removed to 10ppm from 500～20000ppm, and carbon dioxide can be removed to 50ppm from 1～10%.
The present invention is applicable to separation removal ethene and carbon dioxide from the mist that contains ethene, carbon dioxide; Also can be from the mist that contains ethene separation removal ethene.Be specially adapted to separation removal ethene and carbon dioxide from modified atmosphere fresh-keeping storage waste gas, the purified gas of acquisition can return modified atmosphere fresh-keeping storage again and recycle.
Below, with embodiment and accompanying drawing thereof the present invention is further described again.
Description of drawings
Fig. 1 is a kind of schematic flow sheet that evacuation step is arranged that removes the adsorption method of separation of ethene, carbon dioxide from mist of the present invention.
Fig. 2 is the schematic flow sheet towards step of having of the another kind of the present invention adsorption method of separation that removes ethene, carbon dioxide from mist.
The specific embodiment
The adsorption method of separation that removes ethene, carbon dioxide from mist of the present invention, the pressure swing adsorption system that adopts the common adsorbent bed by at least two tower structures, configuring pipes, control valve etc. to constitute is realized this adsorption separating method.The inventive method is filled with adsorbent in adsorbent bed.Evacuation step is arranged in the inventive method and two kinds of rinsing steps are arranged.Table 1 is a kind of time-scale of the present invention that evacuation step is arranged of two bed systems, and Fig. 1 is the process chart of table 1.Table 2 is time-scales of the present invention that rinsing step is arranged of a kind of two bed systems, and Fig. 2 is the process chart of table 2.
Table 1: the time-scale of the present invention that evacuation step is arranged
| Adsorbent bed A | Absorption | The reverse pressure of putting | Find time | Boost | ||
| Adsorbent bed B | The reverse pressure of putting | Find time | Boost | Absorption | ||
Table 2: the time-scale of the present invention that rinsing step is arranged
| Adsorbent bed A | Absorption | The reverse pressure of putting | Flushing | Boost | ||
| Adsorbent bed B | The reverse pressure of putting | Flushing | Boost | Absorption | ||
Be that example describes the inventive method with table 1 and Fig. 1 below.
The gas that contains ethene and carbon dioxide or ethene (for example modified atmosphere fresh-keeping storage waste gas) with certain absolute pressure is by pipeline 10, enter through valve 1A and to be in the adsorbent bed A that adsorbed state promptly moves adsorption step, impurity gas ethene in the gas, carbon dioxide are adsorbed the adsorbents adsorb of loading in the bed, are purified gas and send into modified atmosphere fresh-keeping storage through pipeline 20 again through valve 2A and recycle.Have only 1A, 2A to open with the valve that adsorbent bed A links this moment, and 3A, 4A then are in closed condition.When adsorbent bed A was in adsorbed state operation adsorption step, adsorbent bed B then was in reproduced state and moves all the other steps.At this moment, the adsorbent in the adsorbent bed B has adsorbed ethene or carbon dioxide and ethene, during regeneration of adsorbent beds, at first moves the reverse pressure step of putting, and opens 3B, and valve 1B, the 2B, the 4B that link to each other with adsorbent bed B all are in closed condition.The gas of certain absolute pressure in the adsorbent bed B is discharged outside the tower by pipeline 40, be evacuation step then, open vavuum pump, adsorbent bed is found time, this step also can be a rinsing step, also constantly is evacuated or washes desorb at ethene, the carbon dioxide of this step absorption in service.Be the step of boosting at last, open valve 4B, purified gas progressively boosts to adsorbent bed B through pipeline 30, reaches till the absorption absolute pressure, immediately shut off valve 4B.
Regeneration, technological process and the step etc. of the treating capacity of the pressure swing adsorption system adsorbent bed quantity of each embodiment, the composition and the content thereof that contain the gaseous mixture of ethene, carbon dioxide, the composition that removes ethene, carbon dioxide after-purification gas and content thereof, purified gas, the adsorbent bed quantity of pressure swing adsorption system, adsorbent, adsorbent are following listed.
1, gaseous mixture is formed and content: H
298.95%, C
2H
40.05%, CO
21%.
2, purified gas is formed and content: H
299.994%, C
2H
40.001%, CO
20.005%.
3, purified gas treating capacity: 300Nm
3/ h.
4, adsorbent bed quantity: 2.
5, adsorbent: activated alumina 10%+ active carbon 20%+ Kiselgel A 70%.
6, process flow steps: absorption, the reverse pressure of putting, flushing is boosted.
7, adsorbent reactivation mode: backflow purified gas flushing.Flushing absolute pressure: 0.12MPa.
8, absorption absolute pressure: 0.15MPa.
Embodiment 2
1, gaseous mixture is formed and content: H
294.99%, C
2H
40.01%, CO
25%.
2, purified gas is formed and content: H
299.984%, C
2H
40.001%, CO
20.015%.
3, purified gas treating capacity: 500Nm
3/ h.
4, adsorbent bed quantity: 2.
5, adsorbent: activated alumina 10%+ active carbon 90%.
6, process flow steps: absorption, the reverse pressure of putting is found time, and boosts.
7, adsorbent reactivation mode: vavuum pump is found time.Absolute pressure: 0.007MPa finds time.
8, absorption absolute pressure: 0.3MPa.
Embodiment 3
1, gaseous mixture is formed and content: N
289%, C
2H
41%, CO
210%.
2, purified gas is formed and content: N
299.695%, C
2H
40.005%, CO
20.3%.
3, purified gas treating capacity: 300Nm
3/ h.
4, adsorbent bed quantity: 2.
5, adsorbent: activated alumina 10%+ active carbon 90%.
6, process flow steps: absorption, the reverse pressure of putting is found time, and boosts.
7, adsorbent reactivation mode: vavuum pump is found time.Absolute pressure: 0.01MPa finds time.
8, absorption absolute pressure: 0.4MPa.
Embodiment 4
1, gaseous mixture is formed and content: N
290%, C
2H
42%, CO
28%.
2, purified gas is formed and content: N
299.89%, C
2H
40.01%, CO
20.1%.
3, purified gas treating capacity: 1000Nm
3/ h.
4, adsorbent bed quantity: 4.
5, adsorbent: activated alumina 10%+ active carbon 90%.
6, process flow steps: absorption, once all pressure drops, the equal pressure drop of secondary, the reverse pressure of putting is found time, once all voltage rises, the equal voltage rise of secondary is boosted.
7, regeneration: vavuum pump is found time.Absolute pressure: 0.015MPa finds time.
8, absorption absolute pressure: 0.6MPa.
Embodiment 5
1, gaseous mixture is formed and content: N
296.5%, C
2H
40.5%, CO
23%.
2, purified gas is formed and content: N
299.948%, C
2H
40.002%, CO
20.05%.
3, purified gas treating capacity: 2000Nm
3/ h.
4, adsorbent bed quantity: 4.
5, adsorbent: activated alumina 10%+ active carbon 90%.
6, process flow steps: absorption, once all pressure drops, the equal pressure drop of secondary, the reverse pressure of putting is found time, once all voltage rises, the equal voltage rise of secondary is boosted.
7, adsorbent reactivation mode: vavuum pump is found time.Absolute pressure: 0.025MPa finds time.
8, absorption absolute pressure: 0.8MPa.
Embodiment 6
1, mixes gasification and form content: N
287.5%, C
2H
40.5%, CO
212%.
2, purified gas is formed and content: N
299.895%, C
2H
40.005%, CO
20.1%.
3, purified gas treating capacity: 3500Nm
3/ h.
4, adsorbent bed quantity: 4.
5, adsorbent: activated alumina 10%+ active carbon 90%.
6, process flow steps: absorption, once all pressure drops, the equal pressure drop of secondary, flushing, once all voltage rises, the equal voltage rise of secondary is boosted.
7, adsorbent reactivation mode: flushing.Flushing absolute pressure: 0.2MPa.
8, absorption absolute pressure: 0.6MPa.
Embodiment 7
1, mixes gasification and form content: H
298.95%, C
2H
40.05%, CO
21%.
2, purified gas is formed and content: H
299.994%, C
2H
40.001%, CO
20.005%.
3, purified gas treating capacity: 300Nm
3/ h.
4, adsorbent bed quantity: 2.
5, adsorbent: activated alumina 10%+ active carbon 60%+13X molecular sieve 30%.
6, process flow steps: absorption, the reverse pressure of putting, flushing is boosted.
7, adsorbent reactivation mode: backflow purified gas flushing.Flushing absolute pressure: 0.4MPa
8, absorption absolute pressure: 0.8MPa.
Embodiment 8
1, mix gasification and form content: N2 96.5%, C2H4 0.5%, and CO2 3%.
2, purified gas is formed and content: N2 99.948%, and C2H4 0.002%, and CO2 0.05%.
3, purified gas treating capacity: 3000Nm3/h.
4, adsorbent bed quantity: 8.
5, adsorbent: activated alumina 10%+ active carbon 90%.
6, process flow steps: absorption, once all pressure drops, the equal pressure drop of secondary, three equal pressure drops, four equal pressure drops, the reverse pressure of putting is found time, four equal voltage rises, three equal voltage rises, the equal voltage rise of secondary, once all voltage rises are boosted.
7, adsorbent reactivation mode: find time.Absolute pressure: 0.05MPa finds time.
8, absorption absolute pressure: 1.5MPa.
Embodiment 9
1, mix gasification and form content: N2 89%, C2H4 1%, and CO2 10%.
2, purified gas is formed and content: N2 99.695%, and C2H4 0.005%, and CO2 0.3%.
3, purified gas treating capacity: 4000Nm3/h.
4, adsorbent bed quantity: 8.
5, adsorbent: active carbon.
6, process flow steps: absorption, once all pressure drops, the equal pressure drop of secondary, three equal pressure drops, the reverse pressure of putting, flushing, three equal voltage rises, the equal voltage rise of secondary, once all voltage rises are boosted.
7, adsorbent reactivation mode: flushing.Flushing absolute pressure: 0.6MPa
8, absorption absolute pressure: 2.0MPa.
Claims (10)
1, a kind of ethene that from mist, removes, the adsorption method of separation of carbon dioxide, it is characterized in that in the pressure swing adsorption system of the circular flow of at least two adsorbent beds that are filled with adsorbent, mist is sent into adsorbent bed, each circulation of adsorbent bed has the absorption of experience successively, or all pressure drops are arranged at least once, the reverse pressure of putting, find time or wash, or all voltage rises are arranged at least once, the step of boosting, at adsorption step adsorbents adsorb removing impurities gas and be trapped in the adsorbent bed, obtain purified gas and discharge adsorbent bed, in the reverse pressure of putting, find time or rinsing step adsorbent desorption and regeneration and impurity gas discharged adsorbent bed, above-mentioned adsorbent is an active carbon, aluminium oxide, silica gel, at least a in the molecular sieve.
2, the adsorption method of separation that from mist, removes ethene, carbon dioxide according to claim 1, the absolute pressure that it is characterized in that said adsorption step is 0.10～2.0MPa, the absolute pressure of evacuation step is 0.007～0.05MPa, and the absolute pressure of rinsing step is 0.12～0.6MPa.
3, the adsorption method of separation that from mist, removes ethene, carbon dioxide according to claim 2, it is characterized in that said mist is the modified atmosphere fresh-keeping storage combustion gas, said adsorbent is aluminium oxide and active carbon, and the absolute pressure of said adsorption step is 0.10～0.6MPa.
4, according to claim 1, the 2 or 3 described adsorption method of separations that remove ethene, carbon dioxide from mist, the flushing gas that it is characterized in that said rinsing step is at least a in Purge gas, air, nitrogen, the adsorbent bed purified gas of discharging.
5, according to claim 1, the 2 or 3 described adsorption method of separations that from mist, remove ethene, carbon dioxide, it is characterized in that absorption is experienced in each circulation of said adsorbent bed successively, the reverse pressure of putting, flushing, the step of boosting.
6, the adsorption method of separation that removes ethene, carbon dioxide from mist according to claim 4 is characterized in that absorption is experienced in each circulation of said adsorbent bed successively, the reverse pressure of putting, flushing, the step of boosting.
7, according to claim 1, the 2 or 3 described adsorption method of separations that remove ethene, carbon dioxide from mist, it is characterized in that absorption is experienced in each circulation of said adsorbent bed successively, the reverse pressure of putting is found time, the step of boosting.
8, according to the described adsorption method of separation that from mist, removes ethene, carbon dioxide of claim 4 claim, it is characterized in that absorption is experienced in each circulation of said adsorbent bed successively, the reverse pressure of putting is found time, the step of boosting.
9, according to claim 1, the 2 or 3 described adsorption method of separations that from mist, remove ethene, carbon dioxide, absorption is experienced in the each circulation that it is characterized in that said adsorbent bed successively, once all pressure drops, the equal pressure drop of secondary, the reverse pressure of putting is found time, once all voltage rises, the equal voltage rise of secondary, the step of boosting.
10, according to claim 1, the 2 or 3 described adsorption method of separations that from mist, remove ethene, carbon dioxide, absorption is experienced in the each circulation that it is characterized in that said adsorbent bed successively, once all pressure drops, forward put pressure, the equal pressure drop of secondary, the reverse pressure of putting, flushing, once all voltage rises, the equal voltage rise of secondary, the step of boosting.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102008899A (en) * | 2010-11-30 | 2011-04-13 | 东莞市威迪膜科技有限公司 | Preparation method of solid-liquid separator tube type micro filter membrane |
| CN101088591B (en) * | 2006-06-13 | 2011-04-20 | 气体产品与化学公司 | Pressure swing adsorption process with improved recovery of high-purity product |
| CN103385286A (en) * | 2013-06-28 | 2013-11-13 | 浙江月宫冷链设备有限公司 | Carbon dioxide removing apparatus for air conditioned storehouse |
| CN106698429A (en) * | 2016-12-29 | 2017-05-24 | 四川天科技股份有限公司 | Method for grading concentration of CO2 through pressure swing adsorption |
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| TWI552957B (en) | 2014-12-15 | 2016-10-11 | 財團法人工業技術研究院 | Co2 adsorption and recovery system and method |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1050403A (en) * | 1989-09-19 | 1991-04-03 | 化学工业部西南化工研究院 | Adsorbent for separating carbon monoxide and ethylene by pressure swing adsorption method |
| CN1029552C (en) * | 1991-08-24 | 1995-08-23 | 化学工业部西南化工研究院 | Pressure swing adsorption process for removing carbon dioxide from ammonia plant shift gas |
| FR2758739B1 (en) * | 1997-01-24 | 1999-02-26 | Ceca Sa | IMPROVEMENT IN PSA HYDROGEN PURIFICATION PROCESSES |
| CN1075394C (en) * | 1997-05-29 | 2001-11-28 | 伍仁兴 | Variable-pressure adsorption process for removing CO2 from transformation gas |
| FR2795657B1 (en) * | 1999-07-02 | 2001-09-14 | Air Liquide | AIR PURIFICATION PROCESS BY ADSORPTION ON BARIUM-EXCHANGED ZEOLITE |
-
2003
- 2003-06-06 CN CNB031351271A patent/CN1315563C/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101088591B (en) * | 2006-06-13 | 2011-04-20 | 气体产品与化学公司 | Pressure swing adsorption process with improved recovery of high-purity product |
| CN102008899A (en) * | 2010-11-30 | 2011-04-13 | 东莞市威迪膜科技有限公司 | Preparation method of solid-liquid separator tube type micro filter membrane |
| CN103385286A (en) * | 2013-06-28 | 2013-11-13 | 浙江月宫冷链设备有限公司 | Carbon dioxide removing apparatus for air conditioned storehouse |
| CN106698429A (en) * | 2016-12-29 | 2017-05-24 | 四川天科技股份有限公司 | Method for grading concentration of CO2 through pressure swing adsorption |
| CN106698429B (en) * | 2016-12-29 | 2019-05-07 | 四川天一科技股份有限公司 | A kind of method of pressure swing adsorption and staged concentrate CO2 |
| CN107344058A (en) * | 2017-09-08 | 2017-11-14 | 成都盛利达科技有限公司 | A kind of hydrogen chloride gas advanced purification process of energy-conservation |
| CN107344058B (en) * | 2017-09-08 | 2023-05-26 | 成都盛利达科技有限公司 | Energy-saving hydrogen chloride gas deep purification process |
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