CN1181905C - Variable-pressure adsorption method using auxiliary system - Google Patents
Variable-pressure adsorption method using auxiliary system Download PDFInfo
- Publication number
- CN1181905C CN1181905C CNB021138826A CN02113882A CN1181905C CN 1181905 C CN1181905 C CN 1181905C CN B021138826 A CNB021138826 A CN B021138826A CN 02113882 A CN02113882 A CN 02113882A CN 1181905 C CN1181905 C CN 1181905C
- Authority
- CN
- China
- Prior art keywords
- adsorption
- pressure
- tower
- accessory system
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Separation Of Gases By Adsorption (AREA)
Abstract
The present invention relates to a pressure swing adsorption method using an auxiliary system, which is characterized in that an auxiliary adsorption regeneration cycle system composed of two or more than two adsorption towers is additionally installed on the basis of a main adsorption regeneration cycle system composed of two or more than two adsorption towers; raw gas firstly enters the main system for adsorption, and then the components difficult to adsorb are output; when the concentration of the components easy to adsorb in the main system are ready to exceed standards, the output of the raw gas is switched to the auxiliary system until the concentration of the components easy to adsorb reaches a controllable concentration or equals to the concentration in the raw gas, and then the adsorption is finished; subsequently, other necessary pressure swing adsorption steps can be carried out; the unqualified components difficult to adsorb are output from the main system and are also successively adsorbed in a pressure swing mode to output the qualified components difficult to adsorb after entering the auxiliary system. The present invention not only can simultaneously obtain the high-purity components easy to adsorb and the components difficult to adsorb, but also can increase the yields of the components to the maximum, and can greatly reduce the construction cost and the operation cost of the systems.
Description
One, technical field
The invention belongs to transformation adsorbed gas separation technology field, be specifically related to a kind of pressure swing adsorption method with accessory system, it can make the easier realization of pressure-swing absorption apparatus maximization.
Two, background technology
The gaseous mixture that produces in chemical process owing to can be divided into easy adsorbent component and difficult adsorbent component mostly, thereby can separate it by pressure swing absorption process and reclaim and be used.
For the pressure swing absorption process that can obtain easy adsorbent component and difficult adsorbent component simultaneously, prior art is disclosed one-step method, as CN1195572A.Because easily adsorbent component does not allow to penetrate in a large number adsorbent bed under the condition of one-step method, otherwise will make the adsorption tower outlet by easily adsorbent component pollution, influence the purity of difficult adsorbent component, so the utilization rate of adsorbent is low, the adsorption tower volume is bigger, causes the cost of the system that sets up higher.In order to overcome the defective that one-step method exists, CN1140418A and CN1235862A disclose the method for two kinds of series connection absorption respectively.These two kinds of methods all are that the gas after first order absorption is all adsorbed once more as the unstripped gas of second level absorption, and export difficult adsorbent component product gas from the second level.Obviously, the utilization rate that this has improved adsorbent has to a certain extent improved the purity of difficult adsorbent component, but the saturation depth of first order absorption is not enough, adsorbent does not still make full use of, so the purity of easy adsorbent component also will be carried out pressurized displacement not enough after all pressure finished.As everyone knows, the pressurized displacement process had both taken the systemic circulation time, also was the power consumption process.And, in series connection absorption because the second level is that gas with first order output is all as unstripped gas, this just needs the adsorbent consumption, volume of equipment etc. of second level absorption all supporting with the first order, its cost certainly will be bigger, easily the dividing potential drop of adsorbent component is lower in the unstripped gas of the second level simultaneously, causes the utilization ratio of second level adsorbent not high.
Three, summary of the invention
The objective of the invention is to overcome the defective of prior art, provide a kind of and can obtain easy adsorbent component of high-purity and difficult adsorbent component simultaneously, can improve both yields to greatest extent again, and system cost and the low pressure swing adsorption method of overall energy consumption.
The objective of the invention is by on the basis of an already present main absorption regeneration circulatory system, increase again that an auxiliary absorption regeneration circulatory system reaches.Specifically, be the accessory system that in the presence of the absorption regeneration circulation main system of forming by two or two above adsorption towers, also is provided with an absorption regeneration circulation of also forming by two or two above adsorption towers.During work, the mist that needs to separate recycling at first enters the absorption of main system adsorption tower as unstripped gas, and difficult adsorbent component is discharged by cat head as product gas 1.Carrying out along with absorption, when the easy adsorbent component content in the difficult adsorbent component is 0.01～5%, 1 output of product gas is cut off, substandard product gas 1 switching that makes cat head continue output enters accessory system, easily adsorbent component reaches control concentration or when identical with concentration in the unstripped gas in the gas of main system absorption cat head output, adsorption step finishes, carry out equal pressure drop subsequently successively, find time, all voltage rises and processing step such as dash eventually, and second half section gas that will final all pressure drops and exhaust are as 2 outputs of product gas.After entering the adsorption tower of accessory system by the substandard product gas 1 of main system output, also adsorb successively, all pressure drops, find time, all voltage rises and processing step such as dash eventually, and in adsorption process, export qualified product gas 1 from cat head, final all pressure drops are recovered to main system, and exhaust reclaims as unstripped gas.
If the substandard product gas 1 of main system absorption cat head output is intermittent, can surge tank is set between two systems and collect by surge tank after enter accessory system again and carry out the transformation adsorption treatment.
For the further yield that improves product gas, and reduce the system engineering cost, the present invention has also taked following measure:
1, respectively is provided with void tower in main system and accessory system, number is 0～8, both all press can be between main system and accessory system adsorption tower separately or/and carry out between adsorption tower and the void tower, also can be at the adsorption tower between two systems or/and carry out between the void tower, all pressing number of times is 1～10 time.
2, being in air inlet simultaneously in main system and the accessory system is 1～10 with the adsorption tower number of finding time simultaneously.
In addition, among the present invention in main system and the accessory system separately final all pressure drops and final equal pressure drop each other can be reversely or forward, specifically determine according to technological requirement.When carrying hydrogen or methanol-fueled exhaust and carry hydrogen as conversion gas decarbonization, synthetic ammonia tailgas in Ammonia Production, easily adsorbent component is not because of exporting as product gas 2, final all pressure drops of main system are then adopted reverse, so just can utilize overbottom pressure flushing adsorbent bed in the tower, take away easily adsorbent component of a part, alleviate the load of finding time, reduce the energy consumption of finding time.During as some gaseous mixture adsorbing separation, easily adsorbent component will be as 2 outputs of product gas, and its final all pressure drop is then adopted forward.Especially easy adsorbent component itself has reached higher concentration in gaseous mixture, when final all pressure drops all can directly be exported as product gas 2, also can save the pressurized displacement step, thereby cut down the consumption of energy.As with the coal being the gaseous mixture that the conversion gas of raw material is produced when producing synthetic ammonia, urea, because of the volumetric concentration of its easy adsorbent component CO2 just has 28% approximately, through absorption, all final all pressure drops after the pressure drop, comprise that the CO2 average content in the exhaust just reaches more than 98.5%, thereby can directly export as product gas 2, and need not carry out pressurized displacement again.But, then still need all after the pressure drop pressurized displacement step is set at the final of main system adsorption tower when if easily adsorbent component concentration is low in some gaseous mixture.
The adsorbent of filling can be at least a in activated alumina, active carbon, molecular sieve, the silica gel in the adsorption tower of the present invention; Its filling mode, filling kind, filling combination, filling ratio determine that according to the technic index of unstripped gas composition and the requirement of product gas these all are the known knowledge of present technique field professional during use.
In sum, compared with the prior art the present invention has the following advantages:
1, improved the utilization rate of adsorbent.Because the adsorbent degree of saturation of main system of the present invention is very high, the state that can reach capacity, i.e. adsorption tower outlet is consistent with the easy adsorbent component concentration of inlet, and the adsorbent degree of saturation of one-step method has only 30～50%.Accessory system is owing to only handle the main system substandard product gas 1 after the preliminary treatment, and its treating capacity is far smaller than the second level of series connection absorption, so under the condition for the treatment of capacity equally, the consumption of adsorbent is less among the present invention, its utilization rate is then very high.
2, improved the yield of product gas.Obtained on the basis of most of highly purified difficult adsorbent component at main system absorption cat head of the present invention, on the one hand because the utilization of main system adsorbent is abundant, saturation degree is very high, dead space diminishes in the absorption Tata, thereby improved the yield of difficult adsorbent component, on the other hand also because there is accessory system to continue the associated treatment substandard product gas 1 of preliminary treatment, export qualified difficult adsorbent component, and a part of step-down gas of accessory system returned main system as the gas that boosts, further improved the yield of difficult adsorbent component again.In addition, owing to the adsorbance of the adsorbent commute adsorbent component of utilizing the inventive method is big, corresponding easily adsorbent component emptying amount is just little, also the accessory system exhaust directly can be returned the main system that finishes of just having found time, so the present invention has also improved the yield of easy adsorbent component in addition.
3, improved the purity of product gas.Because the degree of saturation of main system of the present invention is very high, corresponding to easily the concentration of adsorbent component is also just high in the adsorbent, difficult adsorbent component is just purified easily, also has the further underproof difficult adsorbent component of purification of accessory system in addition, so the purity of difficult adsorbent component can be done very highly, otherwise the easy adsorbent component purity that obtains from final all pressure drops and exhaust is also very high.
4, the construction cost and the operating cost of system have been reduced.Because main system degree of saturation of the present invention is than the prior art height, its adsorbent amount ratio is less, corresponding corollary equipment and power consumption also will reduce, accessory system only need be handled main system underproof product gas 1 after the preliminary treatment in addition, treating capacity is far smaller than the second level of series connection absorption, system dimension is also dwindled greatly than the second level of series connection absorption, thereby the construction cost of system and operating cost are all reduced greatly.
5, reduced energy consumption.Because main system degree of saturation height of the present invention, when the easy adsorbent component concentration of unstripped gas was higher, final all pressure drops and exhaust all can not need to carry out pressurized displacement, thereby reduce energy consumption directly as 2 outputs of product gas.Need pressurized displacement after final equal pressure drop even easy adsorbent component concentration is hanged down in the unstripped gas, also the degree of depth because of adsorbent is saturated, makes replacement amount littler than the prior art, and corresponding energy consumption is also less.In addition as easily adsorbent component is as 2 outputs of product gas, as long as equal pressure drop number of times is not many and reverse step-down mode is adopted in final all pressure drops, just can utilize the residual voltage reduction energy consumption of finding time.
6, applied widely.The applicable adsorbing separation with different separation gaseous mixtures of method provided by the invention is as the various conversion gas that need purify, off-gas, coke oven flue gas, air etc. in oil, chemical industry, the metallurgical production process.
Four, the specific embodiment
Also the invention will be further described to provide embodiment below.Be necessary to be pointed out that at this following examples can not be interpreted as limiting the scope of the invention, still belong to protection domain of the present invention if the person skilled in the art in this field makes some nonessential improvement and adjusts the present invention according to the invention described above content.
Embodiment one:
Present embodiment is to be used for methanol-fueled exhaust to carry hydrogen, and unstripped gas pressure is gauge pressure 1.8MPa.Present embodiment adopts is flow process A.62220+B.31114, and promptly main system A is six tower flow processs, wherein two towers air inlet simultaneously, and two towers are found time simultaneously, directly all press, do not have indirectly and all press for twice; Accessory system B is a three-column process flow, wherein single tower air inlet, and single tower is found time, and once directly all presses, and all presses indirectly for four times.In each period of main system and the circulation of accessory system absorption regeneration, the step preface of each tower is shown in table 1,2.
Table 1 A.62220
| A1 | Absorption output hydrogen | Output to the B system | ||||||
| A2 | Twice step-down | Put pressure | Find time | |||||
| A3 | Find time | Boost for three times | Dash eventually | |||||
| A4 | Boost | Dash eventually | Absorption output hydrogen | |||||
| A5 | Absorption output hydrogen | Output to the B system | Twice step-down | Put pressure | ||||
| A6 | Find time | Boost for three times | ||||||
The absorption regeneration cyclic process of present embodiment main system is that example is illustrated with the A1 tower: methanol-fueled exhaust is delivered to A system within battery limit through pipeline, is input to the A system by flow control system.The first step, the A1 tower is in adsorbed state, and impurity is adsorbed in this process, and qualified hydrogen is delivered to product gas surge tank from the top of A1 tower by output valve, and the content of impurity reaches technic index limit, i.e. N in hydrogen
2+ CH
4Content is 0.1% o'clock, and the close outflow valve door is opened and carried valve; Second step, defective gas is delivered to the adsorbent of B system in the A1 tower near saturated along airintake direction by surge tank, adsorbent is fully used, difficult adsorbed gas product hydrogen almost completely penetrates adsorbent; The 3rd step, progressively reduce the pressure of A1 tower along airintake direction by the equalizing valve door at twice, corresponding adsorption tower pressure raises one by one; The 4th goes on foot, and puts by pressure release valve goalkeeper residual gas pressure against airintake direction to be pressed onto near atmospheric pressure, and this process will be taken away a large amount of impurity, and the energy consumption of finding time is reduced greatly; The 5th step, against airintake direction by the desorb of finding time of evacuation valve goalkeeper residual impurity gas; The 6th step, divides 3 times (wherein once from the B system) against airintake direction by progressively the raise pressure of A1 tower of equalizing valve door, the adsorption tower pressure of correspondence reduces one by one; In the 7th step, highly purified hydrogen is charged to absorption pressure towards valve with A1 tower pressure by whole against airintake direction.So go round and begin again.
Table 2 B.31114
| B1 | Absorption output hydrogen | ||||
| B2 | 5 step-downs | Reclaim | Find time | ||
| B3 | Find time | Boost for 4 times | Dash eventually | ||
The absorption regeneration circulation of present embodiment accessory system is that example is illustrated with the B1 tower: the defective hydrogen from the A system is delivered to B system within battery limit through pipeline by surge tank, enters the B system.The first step, the B1 tower is in adsorbed state, and impurity is adsorbed in this process, and qualified hydrogen is delivered to product gas surge tank from the top of B1 tower by output valve, and the content of impurity reaches technic index limit, i.e. N in hydrogen
2+ CH
4Content is 0.1% o'clock, the close outflow valve door; Second step, divide 5 times (wherein once as the gas that boosts of A system) progressively to reduce the pressure of B1 tower by the equalizing valve door along airintake direction, the adsorption tower pressure of correspondence raises one by one; In the 3rd step, be recycled to the A system by equalizing valve goalkeeper residual gas along airintake direction; The 4th step, against airintake direction by the desorb of finding time of evacuation valve goalkeeper foreign gas; The 5th step, divides four times (wherein once delivered to the A system, no longer returned native system) against airintake direction by progressively the raise pressure of B1 tower of equalizing valve door, the adsorption tower pressure of correspondence reduces one by one; In the 6th step, highly purified hydrogen is charged to absorption pressure towards valve with B1 tower pressure by whole against airintake direction.So go round and begin again.
The product hydrogen purity of present embodiment is 99.8%, and yield is 95%.
Embodiment two:
Present embodiment is that the conversion gas that is used for urea production separates, and unstripped gas pressure is gauge pressure 0.8MPa.Present embodiment adopts the A.C4320+B.81131 flow process, and promptly main system A is 12 tower flow processs, wherein four towers air inlet simultaneously, and three towers are found time simultaneously, and two towers are directly all pressed, and do not have indirect pressure equalizing; Accessory system B is eight tower flow processs, single tower air inlet, and single tower is found time, and directly all presses, once all presses indirectly for three times.In each period of main system and the circulation of accessory system absorption regeneration, the step preface of each tower is shown in table 3,4.
Table 3 A.C4320
| A1 | Absorption output hydrogen and nitrogen gas | Output to the B system | ||||||
| A2 | Twice step-down | Put pressure | Find time | |||||
| A3 | Find time | Boost for three times | Dash eventually | |||||
| A4 | Boost | Dash eventually | Absorption output hydrogen and nitrogen gas | |||||
| A5 | Absorption output hydrogen and nitrogen gas | Output to the B system | Twice step-down | Put pressure | ||||
| A6 | Find time | Boost for three times | ||||||
| A7 | Output to the B system | Twice step-down | Put pressure | Find time | ||||
| A8 | Find time | Boost for three times | Dash eventually | |||||
| A9 | Dash eventually | Absorption output hydrogen and nitrogen gas | ||||||
| Aa | Absorption output hydrogen and nitrogen gas | Output to the B system | Twice step-down | |||||
| Ab | Step-down | Put pressure | Find time | |||||
| Ac | Boost for three times | Dash eventually | Absorption output hydrogen and nitrogen gas | |||||
The absorption regeneration cyclic process of present embodiment main system is that example is illustrated with the A1 tower: conversion gas is delivered to A system within battery limit through pipeline, by flow control system input A system.The first step, the A1 tower is in adsorbed state, CO in this process
2Be adsorbed, qualified hydrogen and nitrogen gas is delivered to product gas surge tank, CO in hydrogen and nitrogen gas from the top of A1 tower by output valve
2Content reach technic index limit, promptly 0.2% o'clock, the close outflow valve door was opened and is carried valve; In second step, defective gas is directly delivered to the adsorbent of B system in the A1 tower near saturated along airintake direction, promptly easy adsorbent component CO
2Exit concentration near entrance concentration, adsorbent is fully used; The 3rd step, progressively reduce the pressure of A1 tower along airintake direction by the equalizing valve door at twice, corresponding adsorption tower pressure raises one by one; In the 4th step, put pressure, the CO in putting the body of calming the anger by pressure release valve goalkeeper residual gas pressure along airintake direction
2Content reaches 98.5% o'clock of technological requirement, and residual gas is recovered to CO
2Gas storage holder; In the 5th step, remain CO by the evacuation valve goalkeeper against airintake direction
2Find time desorb and it is recovered to CO of gas
2Gas storage holder; The 6th step, divides three times (wherein once from the B system) against airintake direction by progressively the raise pressure of A1 tower of equalizing valve door, the adsorption tower pressure of correspondence reduces one by one; In the 7th step, highly purified hydrogen and nitrogen gas is charged to absorption pressure towards valve with A1 tower pressure by whole against airintake direction.So go round and begin again.
Table 4 B.81131
| B1 | Absorption | Four step-downs | Put pressure | Find time | ||||
| B2 | Find time | Boost for three times | Dash eventually | |||||
| B3 | Dash eventually | Absorption | Four step-downs | |||||
| B4 | Put pressure | Find time | Boost for three times | Dash eventually | ||||
| B5 | Boost for three times | Absorption | Four step-downs | |||||
| B6 | Four step-downs | Put pressure | Find time | Boost for three times | ||||
| B7 | Find time | Boost for three times | Absorption | |||||
| B8 | Four step-downs | Put pressure | Find time | Boost | ||||
The absorption regeneration cyclic process of present embodiment accessory system is that example is illustrated with the B1 tower: the defective hydrogen and nitrogen gas from the A system is delivered to B system within battery limit through pipeline, enters the B system.The first step, the B1 tower is in adsorbed state, CO in this process
2Be adsorbed, qualified hydrogen and nitrogen gas is delivered to product gas surge tank, CO in hydrogen and nitrogen gas from the top of B1 tower by output valve
2Content reach technic index limit, promptly 0.2% o'clock, the close outflow valve door; Second step, divide four times (wherein once as the gas that boosts of A system) progressively to reduce the pressure of B1 tower by the equalizing valve door along airintake direction, the adsorption tower pressure of correspondence raises one by one; In the 3rd step, reclaim by equalizing valve goalkeeper residual gas along airintake direction; In the 4th step, pass through evacuation valve goalkeeper CO against airintake direction
2The gas desorb of finding time; The 5th step, divides three times (wherein once delivered to the A system, no longer returned native system) against airintake direction by progressively the raise pressure of B1 tower of equalizing valve door, the adsorption tower pressure of correspondence reduces one by one; In the 6th step, highly purified hydrogen is charged to absorption pressure towards valve with B1 tower pressure by whole against airintake direction.So go round and begin again.
The product hydrogen yield of present embodiment is 99%, and the nitrogen yield is 95%, and carbon dioxide content is 0.2% in the product hydrogen and nitrogen gas; The yield of product carbon dioxide gas is 93%, and purity is 98.5%.
Claims (7)
1, a kind of pressure swing adsorption method with accessory system, comprise by two or two absorption regeneration circulatory systems that above adsorption tower is formed, it is characterized in that in the presence of last absorption regeneration circulation main system the accessory system that also has an absorption regeneration of also forming to circulate by two or two above adsorption towers; Mist at first enters the absorption of main system adsorption tower as unstripped gas, difficult adsorbent component is discharged by cat head as product gas 1, when the easy adsorbent component content in the difficult adsorbent component is 0.01～5%, 1 output of product gas is cut off, substandard product gas 1 switching that makes cat head continue output enters accessory system, easily adsorbent component reaches control concentration or when identical with concentration in the unstripped gas in the gas of main system absorption cat head output, adsorption step finishes, carry out equal pressure drop subsequently successively, find time, all voltage rise and whole dashing are waited processing step, and the second half section gas of final all pressure drops and exhaust are exported as product gas 2; After entering the adsorption tower of accessory system by the substandard product gas 1 of main system output, also adsorb successively, all pressure drops, find time, all voltage rises and processing step such as dash eventually, and in adsorption process, export qualified product gas 1 from cat head, final all pressure drops are recovered to main system, and exhaust reclaims as unstripped gas.
2, the pressure swing adsorption method of band accessory system according to claim 1 enters accessory system again after the substandard product gas 1 that it is characterized in that the output of main system absorption cat head is collected by surge tank and carries out the transformation adsorption treatment.
3, the pressure swing adsorption method of band accessory system according to claim 1 and 2 is characterized in that main system and accessory system respectively are provided with void tower, and number is 0～8, and two systems to be in air inlet simultaneously be 1～10 with the adsorption tower number of finding time simultaneously.
4, the pressure swing adsorption method of band accessory system according to claim 3, it is characterized in that all pressing can main system and accessory system separately adsorption tower and adsorption tower between or/and carry out between adsorption tower and the void tower, also can be at the adsorption tower between two systems or/and carry out between the void tower, all pressing number of times is 1～10 time.
5, the pressure swing adsorption method of band accessory system according to claim 1 and 2 is characterized in that in main system and the accessory system that separately final all pressure drops and final equal pressure drop each other are reverse or forward.
6, the pressure swing adsorption method of band accessory system according to claim 3 is characterized in that in main system and the accessory system that separately final all pressure drops and final equal pressure drop each other are reverse or forward.
7, the pressure swing adsorption method of band accessory system according to claim 4 is characterized in that in main system and the accessory system that separately final all pressure drops and final equal pressure drop each other are reverse or forward.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021138826A CN1181905C (en) | 2002-06-17 | 2002-06-17 | Variable-pressure adsorption method using auxiliary system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021138826A CN1181905C (en) | 2002-06-17 | 2002-06-17 | Variable-pressure adsorption method using auxiliary system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1395981A CN1395981A (en) | 2003-02-12 |
| CN1181905C true CN1181905C (en) | 2004-12-29 |
Family
ID=4742848
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB021138826A Expired - Fee Related CN1181905C (en) | 2002-06-17 | 2002-06-17 | Variable-pressure adsorption method using auxiliary system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1181905C (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106256409B (en) * | 2016-08-21 | 2019-09-03 | 杭州东安科技有限公司 | A kind of pressure swing adsorption system |
-
2002
- 2002-06-17 CN CNB021138826A patent/CN1181905C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1395981A (en) | 2003-02-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1083731C (en) | Simulataneous step pressure swing adsorption process | |
| CN1017133B (en) | Process for recovering oxygen enriched gas | |
| CN1017331B (en) | Method for producing high-purity oxygen from air | |
| CN101108295B (en) | Pressure swing adsorption with displacement and recovery steps for removing CO from shift gas2Method (2) | |
| CN104815521A (en) | Ternary component pressure swing absorption separation method based on eight tower parallel connection | |
| CN101219919B (en) | Method for purifying and recycling methyl hydride from garbage landfill gas | |
| CN113350968A (en) | Hydrogen extraction device and process for recovering tail gas components by using synthetic hydrogen | |
| CN100490939C (en) | Process for removing CO2 from conversion gas by pressure swing adsorption method | |
| CN1151957C (en) | Process for extracting high-purity hydrogen from coke oven gas | |
| CN1215624A (en) | Multi-bed vacuum pressure swing adsorption process for extracting hydrogen from hydrogen-contg. mixed gas | |
| CN1850319A (en) | Pressure-changing adsorption method for recovering low-partial-pressure gas | |
| CN1181905C (en) | Variable-pressure adsorption method using auxiliary system | |
| CN1073876C (en) | Pressure swing adsorption process for separating carbon monooxide from carbon monooxide contg. mixed gas | |
| CN104128073A (en) | Novel saturation adsorption process of pressure swing adsorption decarburization and device thereof | |
| CN1100588C (en) | Pressure swing adsorption process for extracting carbon monooxide as fuel from blast furnace waste gas | |
| CN220214437U (en) | Low-energy-consumption PSA air separation nitrogen making device | |
| CN101306300B (en) | Pressure swing adsorption decarbonization technique and device | |
| CN100358849C (en) | Pressure-variation adsorption separation recovering method for mixd gas containing chloroethylene and acetylene | |
| CN1175917C (en) | Single-system one-step series-connected pressure swing adsorption process | |
| CN1235862A (en) | Variable-pressure adsorption separating method for simultaneously purifying easy-to-adsorb phase and difficult-to-adsorb phase | |
| CN1040292C (en) | Gas separation method by pressure swing adsorption for simultaneously preparing two gas products with high-purity and high-yield | |
| CN1042215C (en) | Oxygen generating method based on pressure variation adsorption separation | |
| CN100355484C (en) | Pressure swing absorption decarbonization process and apparatus | |
| CN102160955A (en) | One-stage pressure swing adsorption process in ammonia-urea synthesizing production | |
| CN1302983C (en) | Pressure swing adsorption continuous oxygen generation method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Sichuan Xinhua Technology Co., Ltd. Assignor: Wang Yu Contract fulfillment period: 2005.12.1 to 2015.12.1 contract change Contract record no.: 2009510000132 Denomination of invention: Variable-pressure adsorption method using auxiliary system Granted publication date: 20041229 License type: Exclusive license Record date: 20091023 |
|
| LIC | Patent licence contract for exploitation submitted for record |
Free format text: EXCLUSIVE LICENSE; TIME LIMIT OF IMPLEMENTING CONTACT: 2005.12.1 TO 2015.12.1; CHANGE OF CONTRACT Name of requester: SICHUAN XINHUA SCIENCE AND TECHNOLOGY CO., LTD. Effective date: 20091023 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20041229 Termination date: 20170617 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |