CN1223167A - Method for operation of air prepurifier which takes into account inlet air conditions - Google Patents
Method for operation of air prepurifier which takes into account inlet air conditions Download PDFInfo
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- CN1223167A CN1223167A CN 98125588 CN98125588A CN1223167A CN 1223167 A CN1223167 A CN 1223167A CN 98125588 CN98125588 CN 98125588 CN 98125588 A CN98125588 A CN 98125588A CN 1223167 A CN1223167 A CN 1223167A
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Abstract
The present invention relates to A pressure swing adsorber air prepurifier, which includes that during a determined time period, flow is measured to an adsorber that is coupled to an air inlet. An actual totalized flow to the on-line adsorber is accumulated, based upon the measured flow values. During this time, air feed conditions are monitored and periodically, a maximum totalized flow to the adsorber is calculated, determined, at least in part, based upon the monitored air feed conditions. Periodically, the actual totalized flow value is compared to a current calculated maximum totalized flow value and upon a predetermined relationship therebetween being reached, the on-line adsorber is decoupled from the air inlet and another adsorber is coupled thereto.
Description
The present invention relates to air prepurifier, it uses with cryogenic air separation plant, more particularly, relates to a kind of improving one's methods of air prepurifier that be used to control, and it is considered various air entry conditions and therefore regulates the operation of air prepurifier.
Cryogenic air separation plant needs clean, dry air source, so that can continue and operation safely.This means that moisture and CO2 in the feeding air in the device must be scavenged into quite low level.This removal operation has reduced heat exchanger and has been iced the blocking problem with solid CO2, and this problem often causes the accident that device stops too early.In addition, some hydrocarbons that are included in the feeding air also must be removed.
Feeding air can be removed impurity by suction-operated.Alternating temperature absorption (TSA) and, recently, transformation is adsorbed (PSA) system and has been used to the removal of impurity.The TSA air prepurifier system that is used for air-separating plant has relatively long circulation timei (in hour), and therefore the gas exchange loss between the circulation is not remarkable relatively.On the contrary, PSA circulation timei short relatively (in minute), and their more frequent ventilations mean the relatively significantly loss of compression feeding air.In addition, in the cyclic transformation process, supervene a kind of not normal phenomenon.This is not normal to need the regular hour to offset, thereby causes the further loss of efficient.
The design of PSA prepurifier system is generally based on the specified criteria of concrete application, or more particularly, based on given air-separating plant in the design.Conservatively select design condition, so that under the environmental condition of great majority expectation, obtain desirable productive rate.General selection is suitable for the fixed cycles time of these conditions as far as possible.Certainly, the physical condition of operation will with daytime to evening, one day to another day, change in a season to another season.
All these change the operating characteristics and the efficient that all can influence the PSA clarifier.Can do some adjustment circulation timei at any time.Yet this is often unworkable or be left in the basket just in practical operation.Therefore, the design of system will often will provide than normal or average every day of actual required bigger thickness of bed layer.Therefore, through repeatedly the circulation after will have a certain amount of the material of no use on and be left.Because higher cycle frequency and bigger gas exchange loss have caused higher capital construction cost and higher operating cost.
The application that is used for the PSA air prepurifier of cryogenic air separation plant is set up effectively.As mentioned above, prepurifier is generally fixed circulation timei, and based on the hypothesis to relevant environment and device parameter.Therefore, it is the circulation timei that adsorption capacity that penetrating of CO2 calculated often is used to determine concrete application based on air total flow and key.In addition, for the sake of assurance, calculate this hypothesis of temperature be based on hot weather.This calculating causes fixing a circulation timei, and has only used a part of adsorption capacity of bed material in circulation timei.In case the fixed cycles time is decided, after this it just remains unchanged.
Regularly the example of cycle P SA system is found in U.S. Pat 5,042,994, Smolarek, J., " the improvement control of PSA operation " (" Improved Control of PSAOperations ").The Smolarek process is used the nitrogen product hold-up vessel of a variable-volume, and this container is monitored so that decision variation on request.Circulate in the reduction demand during in adjust, thereby keep the product purity and the pressure of expectation, and under Parking condition, realize the reduction of power consumption and the saving of energy.
Another time control type PSA system the visible U.S. Pat 4,810,265 of example, Lagree etc., " be used for gas separate pressure swing absorption process " (" Pressure SwingAdsorption Proceess for Gas Separation ").This is an improved PSA method, and it can make, and the composition of easier absorption is recovered economically in the feed gas, for example reclaims nitrogen from air.The composition of easier absorption is used as following current purgative gas (Copurge) when higher adsorptive pressure, and the composition that is not easy to adsorb is used for that adverse current under subatmospheric adsorptive pressure is cleaned and adverse current again aeration step be used for initial repressurize.Operating sequence is controlled by time variable.
U.S. Pat 5,258,056, Shirley, A.I., (" PSA System With Product Turndown and PurityControl ") describes a control system " to have the PSA system that product is regulated and purity is controlled ", and when regulating in order to change required product in the PSA system, this control system can keep the purity of expectation.The variation of a sensor monitoring required product gas, a signal that records and a standard relatively change the gas feed speed that enters system then.
U.S. Pat 4,725,293, Gunderson, J., (" Automatic Control for Pressure Swing Adsorption System ") describes a PSA system " to control pressure swing adsorption system automatically ", and it uses a constant circulation timei and a control system to adjust the air input flow rate, only contains the impurity of preset range (in fact just oxygen) and keeps higher relatively nitrogen output flow so that guarantee the nitrogen that produces.
U.S. Pat 4,693,730, Miller G.Q., " transformation adsorbed product purity control method and device " (" Pressure Swing Adsomtion Product Purity Control Methodand Apparatus ") describes a kind of being used for and controls the method for product purity automatically at psa process, thereby can prevent that when raw material changes impurity from penetrating.This method is to detect from the characteristic of following current decompression effluent and take correct measure.Wherein suitable correct measure is: 1. regulate the adsorption step time to control the impurity level in each; 2. regulate following current decompression terminal pressure, penetrate, and/or 3. regulate the amount of the purge gas that each bench grafting is subjected to, with the degree of control regeneration from the impurity of the product end that is controlled at each.
EPA250235, Armond, people such as J.W., " to the improvement of PSA oxygen evolution system system " (" Improvements in and Relating to PSA Oxygen Generating System ") describes a system, when producing oxygen, this system can detect the concentration of adsorbent bed exit oxygen.The output that is near the lambda sensor in each exit is along with discharging the time of function as bed and becoming.This control system is monitored time dependent oxygen concentration, turns on and off the time of bed with decision.
Therefore, an object of the present invention is to provide a kind of improving one's methods of PSA air prepurifier circulation timei that be used to control.
Another object of the present invention provides a kind of PSA air prepurifier method of circulation timei that is used to control, and in the method, carries out continuous control according to the parameter of porch air feed basically.
A further object of the present invention provides a kind of PSA air prepurifier method of circulation timei that is used to control, and this method can make that adsorbent bed obtains to utilize to greatest extent in cycle period.
Transformation absorption (PSA) air prepurifier comprises at least one first absorber and one second absorber and is used to control the controller of the air feed that enters first absorber and second absorber.The present invention is a kind of " in real time " method, is used to control the circulation timei of each absorber, comprises the steps.In one definite period, measure the air mass flow that enters the absorber that links to each other with air intake.Actual total flow to the on-line adsorption device adds up according to the flow value that records.This section is in the period, and the feed conditions (for example temperature, pressure, relative humidity) of monitoring air simultaneously, at least in part, is calculated and determine to flow into the maximum total flow of absorber termly according to the air feed condition of monitoring.Termly actual total flow value and the maximum total flow value that calculated are at that time compared, when reaching predetermined relationship between them, the on-line adsorption device is thrown off from air intake, and another absorber is linked to each other with air intake.The method that is used to control each absorber circulation timei also will be paid attention to: the variation of required load, the ratio of purgative gas and charging and the not normal phenomenon that takes place when adsorber bed conversion.
Figure 1A is the sketch of PSA prepurifier among the present invention.
Figure 1B is a high-level logical flow chart that is used to explain the inventive method.
Fig. 2 A be when controlling circulation at a fixed time and finishing load to the curve map of bed length.
Fig. 2 B be when the circulation by the inventive method control finishes load to the curve map of bed length.
Fig. 3 A controls the air mass flow that flows into when circulation finishes in the bed curve map to the time at a fixed time.
Fig. 3 B flows into air mass flow in the bed to the curve map of time when the circulation by the inventive method control finishes.
Fig. 4 A is the curve map of the pressure of bed porch when the circulation of set time control finishes to the time.
Fig. 4 B is the curve map of the pressure of bed porch when the circulation by the inventive method control finishes to the time.
Fig. 5 A is at the average high temperature of the prepurifier porch curve map with seasonal variations.
Fig. 5 B is the curve map that the average high temperature in the prepurifier porch changed with time every day.
Fig. 6 is in stable load operation, the graph of relation between the circulation timei when feeding temperature and arrival CO2 penetrate.
Be shown among Figure 1A according to PSA preliminary clearning of the present invention system.Air from air compressor aftercooler (not shown) enters system through piping 101, and enters control valve 103 via pipeline 102.Air enters absorber A through piping 106.The adsorbent that water in the feeding air, CO2 and hydrocarbon are adsorbed among the device A is removed, and every kind of above-mentioned impurity is all preferably less than 1ppmv.The air pipeline 107 of flowing through then of cleaning, check (non-return) valve 108, pipeline 109 and pipeline 110 and enter the heat-exchange system of Cryo Equipment.
Simultaneously, from heat-exchange system with surrounding environment roughly the low pressure purge of isothermal enter the PSA system with gas through piping 119,120 and check (non-return) valve 121.It enters absorber B then, impurity in absorber B by desorb.Waste gas leaves absorber B via pipeline 115,113 and control valve 114 and enters in the atmosphere.When varying cyclically, absorber B removes impurity from feeding air, and absorber A is reproduced simultaneously.
The invention provides and a kind ofly make by changing that pressure drop loss reaches minimum method in the PSA prepurifier circulation timei, so that whole adsorption capacities of each prepurifier bed are fully utilized.The adsorption capacity of bed depends on sorbing material and the quantity and the characteristic of the impurity that need remove, the air mass flow and the physical parameter of the bed of flowing through from air, and cleans the flow-rate ratio of usefulness gas to air.For any given known quantity sorbing material that contains, the perhaps PSA system of the mixture of sorbing material can record its adsorption capacity under the condition of temperature, pressure and the humidity of given gas flow by bed, known bed porch.Can record total flow at specific time point (i.e. " breakthrough point ") then, when breakthrough point, a kind of composition of key (as, CO
2) will begin in the outlet effluent, to occur to be starkly lower than the concentration that allows operating limit, be generally less than 1ppmv.
According to the present invention, flowing into adsorber bed maximum total flow (it will determine circulation timei for the PSA prepurifier of giving sizing) can regulate according to air feed temperature, pressure and relative humidity.In addition, it also is subjected to the influence of purgative gas to hydrocarbon and CO2 concentration in the ratio of feeding gas and the air feed stream.Use and a kind ofly change the empirical method of measuring total flow determines to allow to flow through bed before the bed material must be reproduced maximum total flow based on these.
In order to control, can make controller 130 accept the relevant temperature of importing by the sensor cluster 132 that is contained in pipeline 101 porch (T), pressure (P), and the signal of relative humidity (H) according to above-mentioned situation.Flowmeter 134 provides the gas flow value of input controller 130.In addition, controller 130 has many outputs 136, and these outputs are connected to each different control valve (not shown), so that system is carried out loop control.
Shown in following Figure 1B, in the operating process, controller 130 calculates the maximum total flow of (for example) per minute based on main operating condition (casing 150).Actual flow value by controller 130 accumulative totals in this minute is stored (casing 152).When the operation summation of actual flow approximates the operation summation of maximum total flow greatly, or when reaching and have predetermined relation (decision casing 154), on-line adsorption device bed is owing to come self-controller 130 (casing 156) to be applied to the signal on the output 136 and throw off from production line.At this moment, to online adsorber bed of original right and wrong, at this moment it has just become on-line adsorption device bed (casing 158) to valve event intake air circulation, and present non-online bed is reproduced, and circulates once more.
Method of the present invention can although it is less relatively to change numerical value, also allow the different quite significantly variations in temperature that take place with every day and season simultaneously in the variation of 5 to 25 minutes endoadaptation air feed temperature circulation timei, air pressure and relative humidity.Therefore, the inventive method is considered required operating condition and device every day and seasonal variation, and increases economic efficiency under all conditions.Monitoring air feed condition is to find out the water loading of the air that enters absorber.By utilizing adsorber bed maximum adsorption capacity, the corresponding minimum of reducing to of the frequency of varying cyclically.Air loss amount and improved operating efficiency when so, having reduced emptying.
Control the ratio of purgative gas according to the regeneration of air mass flow and adsorption tower, so that make the concrete needs of its equality circuit to air stream.This has guaranteed the suitable and regeneration effectively of adsorbent bed, for use in circulation next time.
When each circulation commutated, the pressure that imports air separator all can change.The especially work of Distallation systm of this variable effect separator.Need the regular hour that destilling tower is overcome and fall interference, and not normally just must compensating by regulating product flow and purity of being caused.By the disturbance that prediction loop changes and and then comes, controller 130 can make the air that is utilized by device reach maximum, and is minimum thereby the influence that varying cyclically is brought becomes.This effect helps stable air flow when varying cyclically.
The present invention can be well suited to the variation to the product requirement.If add to the load minimizing of air-separating plant, then controller 130 sends the signal that perception reduces requirement, and as response, arrived maximum until adsorber bed by loading the circulation timei that prolongs on-line adsorption device bed, and this point can be determined by total air mass flow.It is minimum that this loss that emptying is caused reduces to, thereby and reduced cost.
The operations improvement that the present invention obtains is illustrated by following accompanying drawing.Fig. 2 A shows condition adsorber bed when the circulation of set time control finishes, in prior art.This longitudinal axis has provided the water and the CO of load on the adsorbent
2, with respect to the transverse axis mapping of representing bed length.The left-hand part of load curve is represented the saturation conditions of bed, with respect to water and the CO from the inlet of bed to the active region
2Load curve descends precipitously, then progressively near 0.
The service life of bed is by CO
2Load capacity decision.CO
2Also untapped adsorbent when the right Regional Representative of the active region of curve finishes in circulation.As shown in the figure, untapped part accounts for the sizable part of whole beds.
The operation that Fig. 2 B representative has the PSA system of a circulation of control according to the present invention.It is identical to enter condition given among condition for import and Fig. 2 A of bed.Circulation timei is by entering the air mass flow that bed enters the mouth, pressure, temperature and humidity control.In the case, Chuan unused portion reduces significantly.Method of the present invention allows the adsorber bed maximum that loads to, and the result makes the lower end of load curve still be in and discharges CO in the logistics
2Concentration limit under.
By adding up to the air that flows into prepurifier, this method allows adsorber bed whole entry conditions to reach optimum operation, comprises the variation of air mass flow.Therefore, the variation of device load can be observed at an easy rate, though it is still keeping same high efficiency state.According to this operator scheme, the frequency of varying cyclically becomes minimum, so the emptying loss reduces to minimum equally.Therefore also can obtain the corresponding reduction of energy consumption.
Fig. 3 A and 3B representative enter the adsorber bed air mass flow of PSA.Fig. 3 A is given in an air mass flow in the set time control circulation, and is the same with prior art.Between twice varying cyclically, relatively stable from the air that prepurifier flows out.Yet, when varying cyclically, owing to will therefore make air mass flow reduce suddenly to a bed supercharging in several beds.These compressors are supplied with more air to react to prepurifier.For making this reaction take place to need the limited amount time.Therefore, the initial result who obtains is that flow reduces, and and then is that flow rises rapidly, is the toning (overshooting) of expectation flow at last.Following required flow has set up again.This order causes the labile state of the distillation fraction of air-separating plant, and this state must compensate.
The improvement that the present invention brings is illustrated by Fig. 3 B.It is identical to enter the given condition of initial conditions and Fig. 3 A in the bed.First significant variation is the increase of circulation timei.This causes the minimizing of potential not normal phenomenon in the Distallation systm.The program that controller 130 one of formulation can make the air-flow of air compressor increase before varying cyclically just.Therefore, more air can be used for making adsorber bed repressurize when varying cyclically.Similarly, controller 130 is formulated one and is used to make flow to be reduced to the program of original desirable value, so that over control is limited to minimum degree.Therefore, Zui Xiao flow rate disturbance follows the increase of circulation timei to guarantee comparatively steadily and the more efficient operation pattern.
The order of blower operations is shown among Fig. 4 A and the 4B.These two figure are based on entering adsorber bed identical initial conditions.Fig. 4 A illustrates the pressure based on the adsorber bed porch of the set time control circulation of prior art.Adsorber bedly be pressurized to operating pressure rapidly at first.On-line adsorption device bed keeps pressure stable in the absorption phase of circulation then.When the circulation of set time finished, pressure quickly fell to a low value, at this moment purgative gas can be used for regeneration.When the cleaning phase finished, adsorber bed quilt supercharging once more circulated so that repeat.
Curve among Fig. 4 A can be directly and Fig. 4 B compare, Fig. 4 B is illustrated in according to the operation under the continuous control loop condition of the present invention.Carried out identical operations, still, owing to the adsorbent in the bed is fully utilized, so circulating continuancing time has prolonged.
When being used to control cycle-index, method of the present invention can or enter each or multinomial control in these parameters of air mass flow of PSA prepurifier based on pressure, temperature, humidity.But, when all quadrinomial parameters all are included in the control method, can obtain maximum improvement (with most preferred method).
The design of PSA prepurifier system is generally carried out as follows among the present invention.Normal or average environment condition is considered the residing geographical position of device.Also considered the environmental condition in thinkable hot day.Device must be able to be produced the required product of design flow under these relative harsh conditions.Determine temperature, pressure, humidity and CO for the design of PSA prepurifier then
2Parameter.These conditions can make adsorber bed size decide.
The present invention avoided that adsorber bed most of problem is not utilized in the prior art (when its operation based on the set time circulation time) problem.The change of the operating condition that will consider with the time circulation of not being fixed with the amount of bed does not change.Utilize and a kind ofly carry out cycling, can under the situation of safety that does not jeopardize device and continuous operation, the bed material of maximum is used effectively based on the method for considering feeding air flow, its pressure, temperature and humidity.This has just prolonged circulation timei, thereby has reduced the emptying frequency.Because air loss is less, so operating cost reduces.The present invention also allows the PSA system to have to meet economic scale, thus capital expenditure and operating cost the two all be reduced to a minimum.Experiment
The following actual tests of example on the PSA prepurifier, to carry out under the condition of wide region.The adsorbent bed of PSA prepurifier is made up of activated alumina and sodium Y molecular sieve.The parameter of collecting comprises the inlet temperature and pressure, than load factor, promptly per hour the feed volume (cubic feet) by every square feet of bed cross section, purgative gas to the CO of differing heights place in the ratio of feeding gas, the bed
2With the concentration of acetylene, reach the circulation timei of being obtained when penetrating in the bed exit.
The temperature of using the improvement of the operating aspect that the inventive method brings to be based on to enter the charging in the bed changes along with time every day and changes of seasons.These two kinds of variations in temperature depend on the residing geographical position of concrete device, however, following data represented one has 12 variations in temperature every day, the exemplary device that changes with 52 seasonal temperature, two kinds of variations in temperature, every day with seasonal, be sinusoidal substantially in nature, and be shown among Fig. 5 A and the 5B.Fig. 5 B has reflected the variations in temperature of the every day of experiencing in the hot day of July.
It should be noted that the temperature shown in the figure is actual temperature rather than the environment temperature that enters the air of prepurifier.The air that enters prepurifier had been compressed before entering prepurifier and cooling again.Feeding temperature has reflected the performance of the aftercooler and the cooling system that are used to handle air.
Following table has been described the operation under stable loading condition, and has listed operating data, can find improvement operation of the present invention from these data.
Design condition is utilized of the present invention the putting down of utilizing most of the present invention
Big improvement be worth all improvement values enter prepurifier 115 57 85 inlet air temps (mean value every day) circulation timei (minute) 17.6 32.2 28.2
Fig. 6 shows under stable load operation condition, the relation between the circulation timei when feeding temperature and arrival CO2 penetrate (0.5ppm).
When considering seasonal variations, use method of the present invention to determine to operate circulation timei PSA prepurifier system and will make the adsorber bed best use that obtains.According to the circulation timei that the inventive method is calculated, be that temperature and the seasonal temperature according to average every day changes, rather than be the operating and setting circulation timei in hot day that this just shows that the interior mean circulation time (MCT) of one-year age will prolong 38% shown in Fig. 5 A.
This method is accurately followed the variation of situation every day.Be shown in this method of following variation every day among Fig. 5 B and cause the circulation timei of improvement of additional 11% again on the improved basis of above-mentioned seasonality in operational improvement.
Another parameter that influences adsorber bed load is the ratio of purgative gas to feeding gas.This parameter also is included in this method for use in controlling circulation timei.Operate if purgative gas is brought up to 50% to the ratio of feeding gas by 40%, it is approximately to increase by 30% circulation timei that the thing followed is improved.Also have, if the temperature height of adsorbent bed (as in summer), then available less purge flow is removed the impurity on the adsorbent bed, perhaps further reduces circulation timei if desired, and then constant purgative gas charging will cause shorter circulation timei.The utilization rate of purge flow can be easily by controller 130 controls.
The change of load also will influence the adsorber bed life-span.For example,, under the control condition of circulation timei, use this method so under about 80% load, then can make to prolong about 20% circulation timei if air-separating plant is worked.
Should be appreciated that the description of front is just in order to explain the present invention.Those skilled in the art can design various alternative and improved methods not deviating under the condition of the present invention.Therefore, the present invention will comprise method that all these classes of falling into the claims scope substitute, improved and that change.
Claims (9)
1. one kind is used to control the method that transformation is adsorbed (PSA) air prepurifier, this prepurifier comprises at least one first absorber and one second absorber and is used to control the control device of the air feed that enters first absorber and second absorber that said method comprises the steps:
A) measure the flow that in one definite period, flows into a said absorber that connects together with air intake;
B) according to the flow value that from step a), records, the actual total flow that accumulative total enters a said absorber;
C) monitoring air feed condition;
D) calculate the maximum total flow that enters a said absorber termly, said maximum total flow depends on said air feed condition at least in part; With
E) termly actual total flow value and the maximum total flow value that calculates are compared, when the predetermined relationship that reaches between them, a said absorber is thrown off from said air intake, and second said absorber and said air intake are linked up.
2. the described method of claim 1, wherein said definite time is less than a cycle period to an absorber input air.
3. the described method of claim 2, wherein said monitored air feed condition comprise the temperature that enters the air in the said absorber, enter the pressure of the air in the said absorber and enter at least one parameter in the relative humidity of the air in the said absorber.
4. the described method of claim 1, wherein, in the step e) said predetermined relationship be between them about equally.
5. be used to control acceptance from the system of the circulation timei of transformation absorption (PSA) air prepurifier of the air of air intake, it comprises:
One first absorber and one second absorber;
Be used in one definite period, measuring the device that enters a said absorber flow that links to each other with said air intake;
Be used to monitor the device of the air feed condition that enters said first absorber and said second absorber;
Be used to control the controller of the air feed that enters said first absorber and said second absorber, said controller comprises:
(ⅰ) the mensuration flow value that decides according to input by said measurement mechanism, the actual total flow that accumulative total enters a said absorber;
(ⅱ) calculate the maximum total flow that enters a said absorber termly, said maximum total flow depends on said air feed condition at least in part; With
(ⅲ) actual termly total flow value when the predetermined relationship that reaches between them, is sent a signal, so that a said absorber breaks away from from said air intake, and second said absorber is linked to each other with said air intake.
6. one kind is used to control the method that transformation is adsorbed the circulation timei of (PSA) air prepurifier, this prepurifier comprises at least one first absorber and one second absorber and the control device that is used to control the air feed that enters said first absorber and said second absorber, and said method comprises the steps:
A) measure the flow that in one definite period, flows into a said absorber that connects together with air intake;
B) according to the flow value that from step a), records, the actual total flow that accumulative total enters a said absorber;
C) monitoring air feed condition;
D), a said absorber is broken away from from said air intake, and second said absorber linked to each other with said air intake at least in part according to said total flow; With
E) according to the condition of a said absorber, regulate the purge flow that enters a said absorber, prepare the said time that absorber is required to be reduced to next circulation.
7. the described method of claim 6, wherein step e) is monitored the temperature of a described absorber and is regulated said purge flow in view of the above.
8. the described method of claim 6 if wherein step e) determines that said temperature reduces, then makes said purgative gas flow increase, and if determine that said temperature improves, and then reduces said purgative gas flow.
9. the described method of claim 1, this method also comprises the steps:
F) monitoring is as the air of user's required product; With
G) at least in part according to said user's needs, adjusting enters the flow of the said air feed of a said absorber, prolong a said absorber is broken away from from said air intake and said second absorber is connected to the operation of air intake before time.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101441023A (en) * | 2007-11-23 | 2009-05-27 | 山东科技大学 | Energy-saving type air separation process |
| CN101972582A (en) * | 2010-11-05 | 2011-02-16 | 北京信诺海博石化科技发展有限公司 | Switching method of pressure swing adsorption device for treating non-condensable gas |
| CN105126533A (en) * | 2015-07-23 | 2015-12-09 | 新奥气化采煤有限公司 | Method, apparatus and system for controlling natural gas adsorption column, and purification system |
| CN106422650A (en) * | 2016-09-20 | 2017-02-22 | 深圳市宸瀞环境科技有限公司 | Physical air purification method and device |
| CN110394027A (en) * | 2019-07-23 | 2019-11-01 | 中国石油大学(华东) | The step space division technique that extensive pressure-variable adsorption is coupled with cryogenic separation |
| CN111183213B (en) * | 2017-10-18 | 2021-10-08 | 普莱克斯技术有限公司 | By using ambient CO2Monitoring control of variable adsorption process cycle time |
| CN113941219A (en) * | 2020-07-17 | 2022-01-18 | 气体产品与化学公司 | Radial adsorber, adsorption system and adsorption method |
| CN117463114A (en) * | 2023-12-12 | 2024-01-30 | 成都益志科技有限责任公司 | Automatic determination method for pressure swing adsorption time |
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- 1998-12-17 CN CN 98125588 patent/CN1223167A/en active Pending
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101441023A (en) * | 2007-11-23 | 2009-05-27 | 山东科技大学 | Energy-saving type air separation process |
| CN101972582A (en) * | 2010-11-05 | 2011-02-16 | 北京信诺海博石化科技发展有限公司 | Switching method of pressure swing adsorption device for treating non-condensable gas |
| CN105126533A (en) * | 2015-07-23 | 2015-12-09 | 新奥气化采煤有限公司 | Method, apparatus and system for controlling natural gas adsorption column, and purification system |
| CN106422650A (en) * | 2016-09-20 | 2017-02-22 | 深圳市宸瀞环境科技有限公司 | Physical air purification method and device |
| CN111183213B (en) * | 2017-10-18 | 2021-10-08 | 普莱克斯技术有限公司 | By using ambient CO2Monitoring control of variable adsorption process cycle time |
| CN110394027A (en) * | 2019-07-23 | 2019-11-01 | 中国石油大学(华东) | The step space division technique that extensive pressure-variable adsorption is coupled with cryogenic separation |
| CN113941219A (en) * | 2020-07-17 | 2022-01-18 | 气体产品与化学公司 | Radial adsorber, adsorption system and adsorption method |
| CN117463114A (en) * | 2023-12-12 | 2024-01-30 | 成都益志科技有限责任公司 | Automatic determination method for pressure swing adsorption time |
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