CN1026214C - Producing oxygen enriched product stream - Google Patents
Producing oxygen enriched product stream Download PDFInfo
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- CN1026214C CN1026214C CN 92105494 CN92105494A CN1026214C CN 1026214 C CN1026214 C CN 1026214C CN 92105494 CN92105494 CN 92105494 CN 92105494 A CN92105494 A CN 92105494A CN 1026214 C CN1026214 C CN 1026214C
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Abstract
Disclosed is a two bed pressure swing adsorption process having a high yield and a high production rate. Driving power is saved by utilizing fine or normal size zeolite sieve material and relatively short cycle times and sequencing the various steps of the process to provide substantially continuous use of a vacuum pump.
Description
The present invention relates to by gas mixture that contains oxygen, nitrogen component such as air, obtain the method for oxygen rich air by transformation absorption (PSA).
Pressure swing adsorption system and method have been widely used in from gas mixture (comprising air) preparation oxygen-rich stream, and many this kind system and methods are used.
Utilize in like this system that quite to lack loop cycle be advantageous, this is because of utilizing molecular screen material to adsorb a certain composition in the shorter time well.Short loop cycle is general to use thinner molecular screen material particle size to reduce diffusional resistance.Typical short loop cycle example is asked for an interview United States Patent (USP) 4194891 and 4194892.Adopt above-mentioned patented method can increase oxygen output, but the rate of recovery being quite low, only is 10-20%.
Traditional vacuum PSA method can get higher oxygen recovery rate (50-60%), but productive rate is low slightly.Three traditional PSA method productive rates are not really high; For an example, the bed size factor is 2000-2600kg zeolite/ton oxygen/sky.
Best, people obviously wish by loop cycle and thinner sieve particle faster and obtain high productive rate and obtain the high rate of recovery with traditional more economical simple three bed system methods.
PSA method of the present invention obtains the oxygen enrichment product by the shortcoming that has solved prior art, and it has high oxygen recovery rate and high productive rate, and reduces cost and keep simple operations.
System of the present invention adopts lacks loop cycle and the fine molecular screen material that utilizes, and only needs two beds, thereby has simplified three methods of the high-recovery in the prior art greatly.
Narrate as the back, another feature of the present invention is to utilize continuously or be bordering on the vacuum pump of continuous operation and two adsorption tower systems to save energy consumption.This feature can be finished by carrying out a part or whole part equilibrium process, in this process, supplies with the exit end of second tower from the oxygen-rich stream of the exit end of first tower, separates the sucking-off nitrogen-rich gas from the inlet end of first tower simultaneously.In this way, vacuum pump is moving during partial equilibrium at least and during the remaining step always.Because vacuum pump during full cycle continuously or be close to continuous operation, so its utilization ratio and its watt consumption reach the best.
Therefore, two PSA methods with high-recovery and productive rate are by thin zeolite molecular sieve material particle, as the 20-35 sieve mesh, even larger particles such as 8-12 sieve mesh are being less than 40 seconds, are being preferably in 15-25 and are accomplished in the short cycling time in second.When using vacuum desorption, the pressure oscillating scope is less than 300 torrs, best 200 torrs, and largest production pressure is less than 5psig, preferably less than 3psig.
In the first embodiment of the present invention, this method always is divided into 6 steps to each complete circulation and carries out.Step the first to the 3rd in, first tower is vacuumized continuously by vacuum pump, and in step 4 in step 6, with vacuum pump second tower is vacuumized.So in this embodiment, vacuum pump is using in the cycle in full cycle always.In step 1 and 4, promptly in the pressure equalization step, gas enters another tower through finding time from a tower; In step 2 and 5, the tower of not finding time receives the gas that recharges from the product storage; And in step 3 and 6, the tower of not finding time receives feed-in gas and also produces product, and product gas is used for the purge vacuum column simultaneously.
In second embodiment of the present invention, this method always is divided into 8 steps to each complete circulation and carries out.In step 1 to 4, first tower is vacuumized continuously by vacuum pump, and in step 5 to 8, second tower vacuumized continuously by vacuum pump.Therefore, in this embodiment, vacuum pump is also utilizing in the cycle in full cycle always.In step 1 and 5, promptly in the pressure equalization step, gas enters another tower through finding time from a tower; In step 2 and 6, the tower that does not vacuumize receives from the product storage and recharges gas; In step 3 and 7, the tower of not finding time receives feed-in gas and produces product; And in step 4 and 8, the tower of not finding time continues to receive feed-in gas and also produces product, and product gas is used for the purge vacuum column simultaneously.In other words, the loop cycle of this embodiment except it comprises that the tower that do not vacuumize produces product and another vacuum column is found time and do not had the step of purge, is identical with the circulation of first embodiment.The circulation of recycle ratio first embodiment of this embodiment is more effective.
In the third embodiment of the present invention, this method is carried out 10 steps altogether to each complete loop cycle.First tower is vacuumized continuously by vacuum pump in step 2 to 5, and step 7 to 10 in, second tower vacuumized continuously by vacuum pump.So, in this embodiment, obtain during 8 steps of vacuum pump in 10 steps in operation cycle cycle utilizing.In the step 1 and 6 of pressure equalization step, gas enters another tower from the tower of just finishing product; In step 2 and 7, also be pressure equalization step, wherein gas enters another tower from the tower of finding time; In step 3 and 8, the tower of not finding time receives from the product storage and recharges gas; In step 4 and 9, the tower of not finding time receives feed-in gas and produces product; In step 5 and 10, the tower of not finding time continues to accept feed-in gas, and simultaneously product gas is used for the purge vacuum column.So the loop cycle of this embodiment except it comprises an equilibrium step that does not vacuumize, is identical with the loop cycle of second embodiment.The advantage of this embodiment is to provide in equilibrium process the bed disturbance of gas littler, because when the pressure reduction between bed and the bed reaches maximum, this is in the early stage decompression of not bearing two ends of equilibrium process.
Fig. 1 is a block diagram of the present invention;
Fig. 2 A-Fig. 2 E represents a tower loop cycle of first embodiment of the invention;
Fig. 3 A-Fig. 3 H represents a tower loop cycle of second embodiment of the invention;
Fig. 4 A-Fig. 4 J represents a tower loop cycle of third embodiment of the invention;
The loop cycle of the first embodiment of the present invention is described in detail with reference to the tower loop cycle of schema shown in Figure 1 and Fig. 2.
At first consult Fig. 1 and Fig. 2 A-Fig. 2 F, shown a kind of here from the gas that mainly comprises oxygen and nitrogen such as the system of air continuous production oxygen enriched gas stream.All comprise the sorbent material of adsorption of nitrogen selectively among two adsorption tower A and the B.
In the embodiment of all methods of the present invention, two adsorption towers are loading quite thin zeolite granular, promptly about 8-35 sieve mesh (granularity), preferably about 12-20 granularity.Typical zeolite screen material can use and be spherolite or pill shape (can obtain from various zeolite manufacturers).The control of each step of method embodiment can be regulated with traditional means, as the electromagnetic control valve with the commercial design of timer control criterion.
Shown in Fig. 2 A, valve 1A, 2A close in the first embodiment step 1, thereby the lower end of the isolated first tower A is an inlet end.On the top of tower A is exit end, and valve 4A, 5A close, and valve 3A opens.For the second tower B, valve 9B, 10B close; Thereby the outlet that enters tower A by valve 3A from the gas of tower B outlet, and by valve 8B control air-flow.This moment, the valve 6B of tower B inlet end closed and valve 7B opens in step 1, thus gas from the inlet end of tower B by vacuum pump 16 sucking-offs.
During this step, the pressure of originally high than tower A pressure tower B makes the pressure in two towers equal substantially.In other words, the pressure of tower B can be about 1010 torrs (4.84psig) malleation when step 1 begins, and about 500 torrs when being reduced to step 1 and finishing (5.03psig), and the pressure of tower A is from step 1 that about 200 torrs when initial (10.83psig) rise to 470 torrs (5.61psig).Therefore, when step 1 finished, pressure was in a basic balance between tower.Step 1 is exceedingly fast and carries out, and generally uses 2-6 second, preferably about 4 seconds kinds.
In the step 2, valve 3A closes, valve 5A, 24 open, simultaneously enter the outlet of tower A and recharge tower A, further the raise pressure of tower A by metering valve 26 controls from the oxygen enrichment product gas of storage 18, particularly, because the pressure in the product storage is about 800 torrs, the pressure among the tower A (5.61psig) continues to increase to about 660 torrs (1.93psig) from 470 torrs.Simultaneously, gas is still extracted out from the inlet of tower B by the valve 7B that opens by vacuum pump 16, and the pressure of tower B continues to reduce.In step 2, this pressure can (5.03psig) be reduced to about 450 torrs (6.00psig) from 500 torrs.Equally, compole was short when step 2 was used, was generally 1-5 second, was preferably 3 seconds.
In the step 3, valve 1A opens, and the air inlet that air or other mainly contain oxygen, nitrogen presets the inlet of introducing tower A under the intake pressure by pipeline 14 one.Inlet pressure can change but have the minimum preheating setting pressure value of 3-7psig ideally, is preferably about 5psig.In tower A exit, valve 5A closes, and valve 4A opens, so inlet air flow is adsorbed at this place's nitrogen through tower A, and then the oxygen-rich stream product gas flows through valve 4A from the exit end of tower A, and reverse checkvalve 11 and pipeline 20 arrive product storages 18.During this preparation enriched gaseous oxygen product step, the pressure among the tower A can (1.93psig) increase to about 1010 torrs (4.84psig) from 660 torrs.Simultaneously, in step 3, gas continues to extract out from the tower B desorb or the nitrogen-rich gas of finding time from the inlet end of tower B by vacuum pump 16.Along with the desorb of tower B at its inlet end, valve 10B and 24 opens while oxygen enrichment product stream and is directed to the exit end of tower B with purge column B simultaneously.Oxygen enrichment product gas flow amount is controlled with metering valve 26.Thereby tower B can cause its exit end and purge by oxygen-enriched stream, and the nitrogen concentrated gas is extracted out and desorb from its inlet end simultaneously.Therefore, when the vacuum pump 16 pressure continuous decrease of tower B during continuously pumping incessantly, (6.10psig) reduce to about 200 torrs (10.83psig) from about 450 torrs.Step 3 is also carried out quite soon, is generally 10-25 second cycling time, preferably about 18 seconds.
Then carry out step 4, when the higher pressure strength of tower A was imported tower B, pressure moved towards balance once more.This is undertaken by valve 4A and the open valve 3A that closes tower A exit end.At tower B exit end, valve 10B closes, so gas flow to tower B from tower A, and pressure equilibrium is controlled by metering valve 8B.Simultaneously, the valve 1A that will close tower A entrance end certainly is with cut-out air inlet and open valve 2A, thereby gas can be extracted out via vacuum pump 16 from the entrance end of tower A.The inlet end of tower B is isolated fully because of shut-off valve 7B.
Therefore, in step 4, the pressure approximate equilibrium among tower A, the B, the pressure of tower A reduces to about 500 torrs (5.03psig), and the pressure of tower B (10.83psig) increases to about 470 torrs (5.61) from about 200 torrs from about 1010 torrs (4.84psig).Step 4 is finished in second at about 2-6, best 4 seconds.
In the step 5, valve 3A closes, thereby closes the exit end of tower A fully, and gas continues from the extraction of tower A entrance end pressure is descended, and generally (5.03psig) reduces to 450 torrs (6.00psig) from 500 torrs.Valve 10B, 28 opens, and the oxygen enrichment product enters tower B from product storage 18 and recharges this tower by metering valve 30 controls and just make the pressure the tower B (5.61psig) increase to about 660 torrs (1.93psig) from about 470 torrs.As step 2, recharge step also in 1-5 second, be preferably in about 3 seconds and finish.
In step 6, valve 6B opens at last, thereby will have the air inlet of pressure to introduce tower B inlet.Thereby valve 9B opens the oxygen enrichment product and flows through by reverse checkvalve 12 after pipeline 20 flow to storage 18 from tower B.
In step 6, by metering valve 26 control, valve 24,5A open and allow oxygen rich air to enter the outlet of tower A and purge column A.Simultaneously, along with the purge of tower A, gas continues to discharge with the desorb or the nitrogen-rich gas of finding time from the inlet of tower A by vacuum pump 16.Generally, the pressure of tower A (6.00psig) is reduced to 200 torrs (10.83psig), and the pressure of tower B from about 660(-1.93psig) and increases to about 1010 torrs (4.84psig) from about 450 torrs once more.The carrying out time of step 6 can be 10-25 second, best 18 seconds.
After step 6 is finished, repeating above Overall Steps on the round-robin basis continuously, during each step, continue to obtain the oxygen enrichment product from product storage 18 via valve 32.
Can see that in this embodiment, vacuum pump 16 is to be used to continuously alternately get rid of gas from two towers, thereby can effectively utilize and make the energy consumption of loop cycle to reduce to minimum.
Forward Fig. 3 now to, it has shown a kind of basic round-robin modification shown in Figure 2.Step 1 among Fig. 3,2,5 and 6 is same as the step 1,2,4 and 5 in Fig. 2 circulation respectively.Fig. 3 round-robin step 3 is except tower B washes without the product air-blowing around here, with Fig. 2 round-robin step 3 class.Equally, Fig. 3 round-robin step 7 is different from Fig. 2 round-robin step 6 and is during Fig. 3 round-robin step 7 not purge of tower A.Consequently during Fig. 3 round-robin step 3 maintaining valve 10B and 24 close and during the step 7 maintaining valve 5A and 24 close.
Therefore, in Fig. 3 round-robin step 3, valve 1A opens, and the inlet of tower A is introduced in air or other air inlet that mainly comprises oxygen and nitrogen under predetermined intake pressure.Inlet air pressure can change, but minimum ideally preset value should be between 3 to 7psig, the minimum value of the 5psig that preferably has an appointment.In the exit of tower A, valve 5A closes and valve 4A leaves.Air inlet is by tower A, in tower A nitrogen be adsorbed and oxygen enrichment product stream from its exit end through valve 4A, contrary on valve 11 and pipeline 20 flow into product storages 18.During this step, the pressure among the tower A (1.93psig) is increased to about 900 torrs (2.71psig) from about 660 torrs in producing oxygen enrichment product process.Constantly extract the oxygen enrichment of the desorb or the tower B that finds time during the step 3 out from the inlet end of tower B by vacuum pump 16 gases.So the pressure among the tower B aspirates incessantly by vacuum pump 16, (6.00psig) reduces to about 210 torrs (10.64psig) from about 450 torrs.Step 3 is carried out very soon, circulation time in interval about 8 to 20 seconds usually, and preferably about 13 seconds.
Equally, in Fig. 3 step 7 of cycle period, valve 6B opens, thereby air inlet is introduced tower A through the inlet of tower A.In the exit of tower B, valve 9B opens, and makes whereby from the reverse checkvalve 12, pipeline 20 of flowing through of the oxygen enrichment product among the tower B and flows into product storages 18.During the step 7, the pressure among the tower A (6.00psig) is reduced to about 210 torrs (10.64psig) and the pressure the tower B (1.93psig) is brought up to about 900 torrs (2.71psig) from about 660 torrs from about 450 torrs.The time of step 7 can be 8 to 20 seconds and is preferably 13 seconds.
Fig. 3 round-robin step 4 and 8 except its time ratio Fig. 2 round-robin step 3 and 6 shorter, is identical with Fig. 2 round-robin step 3 and 6.The initial pressure of the tower of finding time in Fig. 3 round-robin step 4 and 8 is lower than the initial pressure of the tower of finding time in Fig. 2 round-robin step 3 and 6, and this is the reason of being found time continuously owing to adsorber in Fig. 3 round-robin step 3 and 7.
Thereby in Fig. 3 round-robin step 4, valve 1A and 4A open, make the oxygen enrichment product among the tower A enter product storage 18 thus through reverse checkvalve 11 and pipeline 20, and in step 8, valve 6B and 9B open, and make the oxygen enrichment product among the tower B flow into product storage 18 through reverse checkvalve 12 and pipeline 20 thus.Valve 7B, 10B and 24 also open in step 4, the tower B that allows oxygen rich gas purge column B thus and vacuum pump 16 is found time continuously.Therefore during step 8, valve 2A, 5A and 24 also open, and allow oxygen rich gas purge column A and allow the vacuum pump 16 tower A that finds time continuously.
During step 4, the pressure among the tower B (10.64psig) drops to about 200 torrs (10.83psig) and the pressure the tower A is increased to about 1010 torrs (4.84psig) from about 900 torrs (2.71psig) from about 210 torrs.Equally, in step 8, the pressure among the tower A (10.64psig) drops to about 200 torrs (10.83psig) and the pressure the tower B is increased to about 1010 torrs (4.84psig) from about 900 torrs (2.71psig) from about 210 torrs.Step 4 and time of 8 can be preferably about 10 seconds from about 5 seconds to 15 seconds.
As seen from last, the total cycle time of this embodiment 16 seconds to 46 seconds scope, is less than 40 seconds the total time of 8 step cycle and is preferably about 30 seconds usually in preferred embodiment.
In this embodiment, vacuum pump 16 also is used for alternately continuously from one of two towers intake-gas, so it can obtain effective use, and makes the power consumption minimum in full cycle.
Forward Fig. 4 now to, shown basic amendment scheme of round-robin shown in Fig. 3 here.Round-robin step 3,4,5,8 among Fig. 4,9 with 10 respectively with Fig. 3 round-robin step 2,3,4,6,7 and 8 identical.Tower B does not vacuumize during the different Fig. 4 of the being round-robin steps 1 of Fig. 4 round-robin step 1 and Fig. 3 round-robin step 1.Equally, tower A did not vacuumize during the step 6 of Fig. 4 was different from Fig. 3 round-robin step 5 and is Fig. 4 round-robin step 6.Consequently during Fig. 4 round-robin step 1 with maintaining valve 7B closed and during its step 6 with maintaining valve 2A closure.Fig. 4 round-robin step 2 and 7 is different from Fig. 3 round-robin step 1 and 5 and only is that the perdurability of these steps and the initial pressure of these steps are inequality.
In Fig. 4 round-robin step 1, valve 3A opens and all other valves (except valve 32) all cut out.During this step, gas is delivered to tower A from tower B.Too during this step, the pressure among the tower A generally (10.83psig) is increased to about 400 torrs (6.96psig) and the pressure the tower B drops to about 750 torrs (0.19psig) from about 1010 torrs (4.84psig) from about 200 torrs.Step 1 is carried out very soon, and it is interior from being about 2 to 6 seconds to be preferably in a cycling time, is preferably 4 seconds.
Equally, in Fig. 4 round-robin step 6, valve 3A opens and other valve (except valve 32) all cuts out.During this step, gas will enter tower B from tower A, and the pressure among the tower B generally (10.83psig) is increased to about 400 torrs (6.96psig) and the pressure the tower A drops to about 750 torrs (0.19psig) from about 1010 torrs (4.84psig) from about 200 torrs.Step 6 also is 2 to 6 seconds generally, is preferably about 4 seconds.
Fig. 4 round-robin step 2 and 7, short and because gas is transferred to from the tower of just finishing product during step 1 and 6 just finishes the regenerated tower makes the initial pressure of rarefied tower Fig. 4 round-robin step 2 and 7 the initial pressure of rarefied tower is hanged down in the step 1 and 5 than Fig. 3 round-robin step except time of its time ratio Fig. 3 round-robin step 1 and 5, they are identical with Fig. 3 round-robin step 1 and 5.
During Fig. 4 round-robin step 1, the pressure among the tower B drops to about 750 torrs from about 1010 torrs (4.84psig), and (0.19psig), the pressure among the while tower A (10.83psig) is increased to about 400 torrs (6.96psig) from about 200 torrs.Equally, during step 6, the pressure among the tower A drops to about 750 torrs (0.19psig) and the pressure the tower B (10.83psig) is increased to about 400 torrs (6.96psig) from about 200 torrs from about 1010 torrs (4.84psig).Step 1 and time of 6 can be preferably about 4 seconds from 2 seconds to 6 seconds.
During Fig. 4 round-robin step 2, the pressure among the tower B (0.19psig) drops to about 500 torrs (5.03psig)) and pressure the tower A (6.96psig) rises to about 470 torrs (5.61psig) from about 400 torrs from about 750 torrs.Equally, during step 7, the pressure among the tower A (0.19psig) drops to about 500 torrs (5.03psig) and the pressure the tower B (6.96psig) rises to about 470 torrs (5.61psig) from about 400 torrs from about 750 torrs.Step 2 and 7 timing can be preferably about 3 seconds from 1 second by 5 seconds.
In this embodiment, vacuum pump 16 is used for replacing intake-gas from one of two towers or another during 8 steps of 10 steps of this round-robin continuously.Thereby it is effectively utilized and almost energy consumption to be reached during the full cycle minimum.During the step that those vacuum pumps are not used for tower is vacuumized, as long as being added to this pump of pump, air just can continue operation if necessary.
Therefore the total cycle time of this embodiment arrived in about 51 seconds scope at about 17 seconds usually.In preferred embodiment, the total time of 10 step cycle is lower than 40 seconds, and ideal is 30 seconds.
The present invention can be further with example explanation down, and wherein unless otherwise indicated, percentage ratio and ratio are all by volume.
Example 1
Use device shown in Figure 1 and sequence of steps shown in Figure 2, carry out program of the present invention to obtain oxygen enrichment product stream.The diameter of two adsorption tower A and B is 2 inches, high 15 inches, operation 1-3 circulation time, the 0.4-0.8mm spherulitic calcium X zeolite molecular sieve material that interior filling can be purchased from Laporte company, and the zeolitic material of the 1.5mm ball shape that filling is buied from Tosoh company (Tosoh Zeolum SA) in circulation 4.Cycle period the transformation scope be that 3.5psig is to 200 torrs.
Cycling time, the rate of recovery and output are listed in table 1.
Table 1
Circulation sequence number 1234
Cycling time (second) 25 20 17 25
Oxygen purity (%) 93 93 93 93
Loose density (kg/cm
3) 181 681 681 620
The oxygen rate of recovery (%) 59 58 56 55
(40 51 59 40 of the preparation of specific product
Oxygen/bed volume rises the standard of number
Rise/per hour)
(every day, oxygen 535 420 375 487 for the bed size factor
Amount of zeolite kg per ton)
, continue that during each step a tower or another tower are applied vacuum and then can obtain the high rate of recovery, high product as seen by two Tower Systems from above test.Vacuum pump is effectively utilized, and therefore, has reduced energy consumption.Circulation is exceedingly fast, and can utilize molecular sieve material soon.Three bed systems that the structure of obvious two bed systems and operating ratio are complicated and expensive have more advantage.
Example 2
Use device shown in Figure 1 and step preface shown in Figure 3, carry out method of the present invention to obtain oxygen enrichment product stream.Adsorption tower A and B diameter are 24 inches, and length is 4 feet.Be filled with 25 inches Tosoh SA500 molecular sieve and 6 inches alumina in the tower, and alumina places the inlet end of tower to absorb moisture.Run duration is enough to set up steady state.
Cycling time, productive rate and the rate of recovery are listed in table 2.
The step time, second
1 and 54
2 and 63
3 and 7 13
4 and 8 10
Product purity (% oxygen) 93.1
The rate of recovery (%) 44.7
Special product (Nm
3/ hr produces
Thing/m
3Molecular sieve) 40.1
As shown in table 2, use the circulation of this embodiment of the invention, can obtain the high product purity and the good rate of recovery.
Example 3
Use device shown in Figure 1 and step shown in Figure 4, carry out method of the present invention to obtain oxygen enrichment product stream.Adsorption tower A and B internal diameter are 4.3cm, long 1.8 meters.The about 1.7 meters Tosoh SA500 molecular sieve of loading height in the tower.In the present embodiment, use giving of about 30cm alumina of filling to put guard bed absorption moisture in each tower.Whether be disturbed the top surface of adsorbent bed sprayed coating before test in cycle period in order to measure bed.After finishing, test looks at the whether complete surface of detecting bed of not moving of dope layer.The surface of fracture shows that bed has disturbance.
Cycling time, productive rate and the rate of recovery are listed in table 3.
Table 3
The step time, second
1 and 64
2 and 73
3 and 83
4 and 9 10
5 and 10 10
Product purity (% oxygen) 93
The rate of recovery (%) 49.2
Specific product (Nm
3/ hr product/m
3Molecular sieve) 41
As seen can obtain the good impact of performance.Find no disturbance behind the surface inspection of bed, this shows that adsorbent bed does not move.Do not having when same test to carry out under the situation of step 1 and 6, checking that measuring bed is subjected to some disturbances.Thereby 10 step cycle of the present invention have additional advantage.
Although embodiments of the invention represent, should understand that the present invention is not limited thereto, people also can carry out different improvement, but these variations will drop within appending claims spirit and the scope.
Claims (22)
1, a kind of utilization contains two adsorption towers of the sorbent material of selecting adsorption of nitrogen and a product storage from containing the method that the air inlet of oxygen, nitrogen at least prepares oxygen enrichment product stream, it is characterized in that comprising that step is:
(i) gas is caused first adsorption tower outlet that is in low pressure from the outlet of second adsorption tower of elevated pressures,, make the pressure balance substantially in two towers when at deflated simultaneously from the inlet end of second tower;
(ii) after step 1 balance, the product gas that places the product storage to be in elevated pressures is caused the outlet of first tower, so that continue to recharge first tower between second tower inlet exhaust cycle, the inlet from second tower continues exhaust simultaneously;
(iii) under predetermined pressure, air inlet is introduced the inlet of first tower and the oxygen rich air product is reclaimed and described oxygen-rich stream is caused the product storage from the outlet of first tower, simultaneously portion of product stream is caused the outlet of second tower with purge second tower and simultaneously from second tower inlet discharge gas, the nitrogen concentrated gas of the desorb and second tower of finding time;
(iv) with gas from the outlet that is in highly compressed first tower outlet at first and causes second tower with the pressure balance two towers substantially, simultaneously with the inlet discharge of gas from first tower;
(v) step after (iv) balance is finished causes the outlet of second tower with the oxygen rich gas product of elevated pressures in the product storage, continues simultaneously gas is discharged from the inlet of first tower;
(vi) air inlet is introduced the inlet of second tower under the described predetermined pressure and reclaimed the oxygen rich air product so that described oxygen-enriched stream is caused the product storage from the outlet of second tower, the outlet that simultaneously portion of product gas is caused first tower is with purge first tower; Meanwhile gas is discharged and from the first tower desorb, the rich nitrogen of finding time from first tower inlet;
(vii) repeating step (i)-(vi), oxygen rich air is taken out use from the product storage simultaneously circularly.
2, the method for claim 1 it is characterized in that the air of described air inlet for about 3-7psig, and described sorbent material is the zeolite grain of 8-35 sieve mesh.
3, method as claimed in claim 2 is characterized in that described zeolite grain is spherolite or pill shape, is of a size of about 12-20 sieve mesh.
4, the method for claim 1 is characterized in that described step (ⅰ) and (ⅳ) carrying out in second at about 2-6; Described step (ⅱ) reaches (ⅴ) carries out in second at about 1-5.Described step (ⅲ) reaches (ⅵ) carries out in second at about 10-25.
5, method as claimed in claim 4 is characterized in that described step (ⅰ) and (ⅳ) carrying out in about 4 seconds; Described step (ⅱ) reaches (ⅴ) carried out in about 3 seconds; Described step (ⅲ) reaches (ⅵ) carried out in about 18 seconds.
6, the method for claim 1, it is characterized in that described step (ⅰ) and (ⅳ) comprise the pressure equilibrium that makes in the tower from about 470 to about 500 torrs; Described product gas is introduced by the pressure with about 800 torrs in step (ⅱ) and (ⅴ); Described air inlet pressure with about 3-7psig in step (ⅱ) reaches (ⅵ) is introduced.
7, method as claimed in claim 6 is characterized in that the pressure of described air inlet less than 5psig.
8, the method for claim 1 is characterized in that described step (ⅰ) to step (ⅳ) process is less than 40 seconds.
9, a kind ofly utilize two adsorption towers that contain the sorbent material of selecting adsorption of nitrogen and a product storage and, it is characterized in that comprising that step is from containing the method that the air inlet of oxygen, nitrogen at least prepares oxygen enrichment product stream:
(ⅰ) when also simultaneously at deflated from the inlet end of second tower, gas is caused first adsorption tower outlet that is in low pressure from second adsorption tower outlet of elevated pressures, make the pressure balance substantially in two towers;
(ⅱ) after step 1 balance, the product gas that places the product storage to be in elevated pressures is caused the outlet of first tower, so that recharge first tower; Inlet from second tower continues exhaust simultaneously;
(ⅲ) inlet mouth is introduced first tower with predetermined pressure, discharges oxygen-rich stream and described oxygen-rich stream is collected into the product storage from the outlet of first tower simultaneously, simultaneously from the inlet discharge gas of second tower with desorb and find time from the nitrogen-rich gas of second tower;
(ⅳ) portion of product is flow to outlet into second tower with purge second tower, simultaneously air inlet constantly introduce first tower of predetermined pressure inlet, discharge oxygen-rich stream, oxygen-rich stream taken in described product storage and discharged gas with desorb and find time from the nitrogen-rich gas of second tower from the inlet of second tower simultaneously from the outlet of first tower;
(ⅴ) with gas from the outlet that is in highly compressed first tower outlet at first and causes second tower in fact in order to the pressure balance two towers, simultaneously with the inlet discharge of gas from first tower;
After (ⅵ) step (ⅴ) balance is finished, the oxygen rich gas product of elevated pressures in the product storage is caused the outlet of second tower, continue simultaneously gas is discharged from the inlet of first tower;
(ⅶ) air inlet is introduced the inlet of second tower with predetermined pressure, simultaneously from the outlet exhaust oxygen-rich stream of second tower and described oxygen-rich stream income product storage, simultaneously from the inlet discharge desorption of gases of first tower and find time from the nitrogen-rich gas of first tower;
(ⅷ) outlet purge first tower that portion of product stream is introduced first tower simultaneously air inlet constantly introduce second tower of predetermined pressure inlet, from the outlet of second tower discharge oxygen-rich stream, oxygen enrichment income product storage and the gas of constantly discharging first tower inlet with desorb and find time from the nitrogen-rich gas of second tower; With
(ⅸ) repeating step (ⅰ)-(ⅷ) circularly takes out use with oxygen rich air simultaneously from the product storage.
10, method as claimed in claim 9 is characterized in that the air of described air inlet for about 3-7psig, and described sorbent material is the zeolite grain of about 8-35 sieve mesh.
11, method as claimed in claim 10 is characterized in that described zeolite grain is spherolite or pill shape, is of a size of about 12-20 sieve mesh.
12, method as claimed in claim 9 is characterized in that described step (ⅰ) and (ⅴ) carries out in second about 2-6; Step (ⅱ) and (ⅵ) carry out in second about 1-5; Step (ⅲ) and (ⅶ) carry out in second about 8-20; And step (ⅳ) and (ⅷ) carry out in second about 5-15.
13, method as claimed in claim 12 is characterized in that described step (ⅰ) and (ⅴ) carried out in 4 seconds; Step (ⅱ) and (ⅵ) in 3 seconds, carry out; Step (ⅲ) and (ⅶ) in 3 seconds, carry out; And step (ⅳ) and (ⅷ) in 10 seconds, carry out.
14, method as claimed in claim 13 is characterized in that the pressure of described air inlet less than 5psig.
15, method as claimed in claim 9 is characterized in that described step (ⅰ) to step (ⅷ) process is less than 40 seconds.
16, a kind ofly utilize two adsorption towers that contain the sorbent material of selecting adsorption of nitrogen and a product storage and, it is characterized in that comprising that step is from containing the method that the air inlet of oxygen, nitrogen at least prepares oxygen enrichment product stream:
(ⅰ) gas is caused first adsorption tower outlet that is in low pressure from the outlet of second adsorption tower of elevated pressures;
(ⅱ) pressure of outlet up to two towers that gas is continued to introduce described first adsorption tower from the outlet of described second adsorption tower till the balance, is constantly discharged gas from the inlet of second tower basically simultaneously;
(ⅲ) after step (ⅱ) balance, the product gas that places the product storage to be in elevated pressures is caused the outlet of first tower, so that recharge first tower, the inlet from second tower continues exhaust simultaneously;
(ⅳ) air inlet is introduced first tower with predetermined pressure, discharges oxygen-rich stream and described oxygen-rich stream is collected into the product storage from the outlet of first tower simultaneously, simultaneously from the inlet discharge gas of second tower with desorb and find time from the nitrogen-rich gas of second tower;
(ⅴ) portion of product is flow to outlet into second tower with purge second tower, simultaneously air inlet continue with predetermined pressure introduce first tower inlet, discharge oxygen-rich stream, oxygen-rich stream taken in described product storage and discharged gas with desorb and find time from the nitrogen-rich gas of second tower from the inlet of second tower simultaneously from the outlet of first tower;
(ⅵ) gas is caused second adsorption tower outlet that is in low pressure from the outlet of first adsorption tower of elevated pressures;
(ⅶ) gas is continued to introduce the outlet of described second adsorption tower from the outlet of described first adsorption tower, the pressure in two towers till the balance, is discharged gas from the inlet of first tower basically simultaneously;
After (ⅷ) step (ⅶ) balance is finished, the oxygen rich gas product of elevated pressures in the product storage is caused the outlet of second tower, continue simultaneously gas is discharged from the inlet of first tower;
(ⅸ) air inlet is introduced the inlet of second tower with predetermined pressure, discharges oxygen-rich stream and described oxygen-rich stream income product storage from the outlet of second tower simultaneously, simultaneously from the inlet discharge gas of first tower with desorb and find time from the nitrogen-rich gas of first tower;
(ⅹ) portion of product stream is introduced the outlet of first tower with purge first tower, simultaneously air inlet continue with predetermined pressure introduce second tower inlet, from the outlet of second tower discharge oxygen-rich stream, oxygen enrichment income product storage, the gas of discharging first tower inlet simultaneously is with desorb and find time from the oxygen enrichment of second tower; With
(ⅹ ⅰ) be repeating step (ⅰ)-(ⅹ) circularly, simultaneously oxygen rich air is taken out use from the product storage.
17, method as claimed in claim 16 is characterized in that the air of described air inlet for about 3-7psig, and described sorbent material is the zeolite grain of about 8-35 sieve mesh.
18, method as claimed in claim 17 is characterized in that described zeolite grain is spherolite or pill shape, is of a size of about 12-20 sieve mesh.
19,, it is characterized in that described step (ⅰ) and (ⅵ) carry out in second about 2-6 as method as described in the claim 16; Step (ⅱ) and (ⅶ) carry out in second about 1-5; Step (ⅲ) and (ⅷ) carry out in second about 1-5; Step (ⅳ) and (ⅸ) carry out in second about 8-20; And step (ⅴ) and (ⅹ) carry out in second about 5-15.
20,, it is characterized in that described step (ⅰ) and (ⅴ) in 4 seconds, carry out as method as described in the claim 19; Step (ⅱ) and (ⅵ) in 3 seconds, carry out; Step (ⅲ) and (ⅶ) in 3 seconds, carry out; Step (ⅳ) and (ⅸ) in 10 seconds, carry out; And step (ⅴ) and (ⅹ) in 10 seconds, carry out.
21, as method as described in the claim 20, it is characterized in that described air inlet is about 5psig pressure.
22, as method as described in the claim 16, it is characterized in that described step (ⅰ) to the time that (ⅹ) carries out altogether is less than 40 seconds.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US07/724,672 US5122164A (en) | 1990-03-29 | 1991-07-02 | Process for producing oxygen enriched product stream |
| US07/724,672 | 1991-07-02 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1069206A CN1069206A (en) | 1993-02-24 |
| CN1026214C true CN1026214C (en) | 1994-10-19 |
Family
ID=24911382
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 92105494 Expired - Fee Related CN1026214C (en) | 1991-07-02 | 1992-07-02 | Producing oxygen enriched product stream |
Country Status (6)
| Country | Link |
|---|---|
| JP (1) | JP3287607B2 (en) |
| CN (1) | CN1026214C (en) |
| AU (1) | AU662909B2 (en) |
| CA (1) | CA2072905C (en) |
| NZ (1) | NZ243350A (en) |
| ZA (1) | ZA924901B (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3654661B2 (en) * | 1994-06-02 | 2005-06-02 | 大陽日酸株式会社 | Oxygen generation method by pressure fluctuation adsorption separation method |
| KR100450284B1 (en) * | 2002-03-28 | 2004-10-02 | 희 철 장 | Gas generator of absorption system |
| KR101499694B1 (en) | 2013-06-28 | 2015-03-11 | 한국에너지기술연구원 | Oxygen adsorbent for easy desorption of oxygen and preparation method thereof |
| US11167260B2 (en) | 2013-06-28 | 2021-11-09 | Korea Institute Of Energy Research | Oxygen selective adsorbent for easy desorption and preparation method thereof |
| KR101671180B1 (en) | 2014-12-30 | 2016-11-02 | 한국에너지기술연구원 | Mid-Temperature Oxygen Selective Adsorbent And Preparation Method Thereof |
| CN112691454A (en) * | 2020-12-15 | 2021-04-23 | 李勇 | Air source filtering device and oxygen generating device |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4810265A (en) * | 1987-12-29 | 1989-03-07 | Union Carbide Corporation | Pressure swing adsorption process for gas separation |
| JP2683806B2 (en) * | 1988-03-17 | 1997-12-03 | 住友精化株式会社 | Concentrated oxygen recovery method |
| EP0380723B1 (en) * | 1989-02-01 | 1994-04-06 | Kuraray Chemical Co., Ltd. | Process for separating nitrogen gas by pressure swing adsorption system |
-
1992
- 1992-06-26 AU AU19313/92A patent/AU662909B2/en not_active Ceased
- 1992-06-29 NZ NZ24335092A patent/NZ243350A/en unknown
- 1992-07-01 ZA ZA924901A patent/ZA924901B/en unknown
- 1992-07-02 JP JP17569992A patent/JP3287607B2/en not_active Expired - Fee Related
- 1992-07-02 CA CA 2072905 patent/CA2072905C/en not_active Expired - Fee Related
- 1992-07-02 CN CN 92105494 patent/CN1026214C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JP3287607B2 (en) | 2002-06-04 |
| NZ243350A (en) | 1994-06-27 |
| CN1069206A (en) | 1993-02-24 |
| JPH05184851A (en) | 1993-07-27 |
| ZA924901B (en) | 1993-04-28 |
| CA2072905A1 (en) | 1993-01-03 |
| AU1931392A (en) | 1993-01-07 |
| CA2072905C (en) | 1999-08-31 |
| AU662909B2 (en) | 1995-09-21 |
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