CN1309455C - Gas concentration method and its apparatus - Google Patents
Gas concentration method and its apparatus Download PDFInfo
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- CN1309455C CN1309455C CNB2004800000114A CN200480000011A CN1309455C CN 1309455 C CN1309455 C CN 1309455C CN B2004800000114 A CNB2004800000114 A CN B2004800000114A CN 200480000011 A CN200480000011 A CN 200480000011A CN 1309455 C CN1309455 C CN 1309455C
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- 239000001301 oxygen Substances 0.000 claims abstract description 24
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
- B01D53/0476—Vacuum pressure swing adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/402—Further details for adsorption processes and devices using two beds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
- B01D53/0446—Means for feeding or distributing gases
Abstract
The present invention relates a method for concentrating a gas by applying a pressure difference to an adsorbent and an apparatus therefor, and particularly, a method for producing an enriched gas in a large amount by introducing a continuous production into every step of the process focusing on productivity rather than concentration of the product gas and an apparatus therefor. The present invention relates to a method incorporating the vacuum swing adsorption method with the pressure swing adsorption method, particularly the rapid pressure swing adsorption method which can continuously produce a desired material in a depressurization step to improve recovery rate of the desired material and productivity and an apparatus therefor. The apparatus according to the present invention is advantageously applied in a small size machine rather than for industrial uses. Particularly, when applied in a small size oxygen concentrator, it can be used in electric home appliances, air conditioners and water purifier, as well as medical products.
Description
The background of invention
1. technical field
The present invention relates to a kind of method and device thereof of producing the concentrated gas that increases specific gas concentration, this method comprises by difference of extra pressure on the adsorbent that specific gas is had selective adsorption capacity separates specific gas from raw gas mixture.
2. background technology
The method for concentration that uses adsorbent to increase specific gas concentration generally is divided into the method for the difference of utilizing gas process speed after additonal pressure on the gas separation membrane and utilizes PSA (pressure swing adsorption method) method of zeolite molecular sieve (ZMS) or carbon molecular sieve (CMS), in pressure swing adsorption method the container that molecular screen material is housed is exerted pressure after the difference, the gas of special component is adsorbed agent absorption, and the weak composition of adsorptivity is separated relatively simultaneously.Pressure swing adsorption method has been widely used in various fields after being introduced by Skarstrom.
The PSA mode in normal pressure (atmospheric pressure) or the above adsorbed gas of normal pressure, is carried out desorb and regeneration at atmospheric pressure usually.Since generation nineteen fifty, the PSA method that grows up gradually is widely used in the suitability for industrialized production of oxygen and nitrogen, also is used for undersize item such as water purifier, air-conditioner and medical instruments and air drying, oxygen concentration and hydrogen purification recently.The oxygen that obtains with the PSA method is widely used in the industry of continuous consumption oxygen, specifically as the electric furnace steel making technology, air fed wastewater treatment, association with pulp bleaching, ozone generator of waste water etc.Recently, the gas that is rich in oxygen replaces the burning that air is used for low nitrogenize (NOx) and efficient purpose and neutralizes biochemical field as fermenting.Especially, oxygen concentrator has been used for household appliances that office and family are carried out air conditioning.Fig. 1 has shown the typical Skarstrom circulation of PSA standard four step process that use two adsorbent beds.Wherein Pl and Ph represent the relatively low pressure value and the high-voltage value of operating pressure respectively.This technology comprises requisite feed pressurization step, blowdown step and purge step.Adsorb and blowdown step and cleaning step are carried out desorb in feed pressurization step.Typical O
2-PSA technology is documented in US3, and 430,418; 4,589,888; In 4,650.501 and 4,981,499.On the standard technology basis, can increase and all press the step to form multistep technology.Such multistep technology may exist the fluctuation of some discharge pressures, therefore needs to increase the quantity of adsorbent bed to reduce the deviation of fluctuation.Though multibed system efficient height has limitation when realizing miniaturization.Though but the PSA device helps medical high concentration systems is unfavorable for the output to be purpose rather than to be the purpose household electrical appliance with concentration.Also have, there is the high relatively shortcoming of initial stage manufacturing cost in it.
For example, traditional approach shown in Figure 7 (JP-A-No.08-239204), not only charging aperture need a plurality of valves (14,12a, 17a, 12b, 17b), and products export also need a plurality of valves (110a, 110b).In addition, the cable bond 112 that connects adsorbent bed A and B need be provided with conversion valve 113, also has cable bond 112 to be provided with to have the circuitous of locking device 114 all to press route 115, and this makes structure complicated.
PSA technology is subdivided in atmospheric pressure or the original PSA type more than the atmospheric pressure according to operating pressure, at atmospheric pressure or more than the atmospheric pressure and the VPSA type of operating between the vacuum pressure and in atmospheric pressure or the VSA type operated below the atmospheric pressure, VSA type and VPSA type can intersect use, or are referred to as PSA.The example of V (P) SA type is documented in US5,122,164; In 5,223,004 and 5,246,676.
The representative factor of evaluation of PSA is concentration, the rate of recovery and productivity ratio, and what technological design and system designing institute were considered in conventional method mainly is the initial investment and the operation cost of concentration, the rate of recovery, factory building because they at be commercial Application.The RPSA of the 1970's exploitation (PSA fast) is the technology at the output exploitation of product gas, this technology utilization is full of the pressure drop of the adsorbent bed generation of fine granular and produces big several times oxygen rich gas, unlike most of PSA, the pressure drop of adsorbent bed inside does not almost have or is out in the cold.That is, different with common PSA technology, owing to produce continuously needed gas, so can improve the rate of recovery of desired gas and improve the productivity of adsorbent in blowdown step.Fig. 2 shows the standard three step process of RPSA, comprises pressurization step, postpones step and washing blowdown step, can omit as required as the delay step of middle spacer step.As shown in Figure 2, produce in each step independently and to carry out continuously, and pressurization step and blowdown step took place in short time in several seconds.The exemplary of RPSA is documented in US4, and 406,675; US5,827,358; US6 is in 068,680 and US6,565,627.Though the emergency oxygen apparatus when these methods are applicable to flight is industrial with some, is not suitable on the commercialization small size home appliance.
To inserting the small-scale production ability concentrater of domestic air cleaner or air-conditioner since the final oxygen concentration of object space to be human body sensory comfortable about 21～23%, so in fact industrial high concentration is skimble-skamble.For water purifier, well-known 50% or the oxygen of higher concentration be enough to increase the oxygen that is dissolved.Therefore, the employing device that can reach large-duty RPSA method is not well suited for the minicomputer device.
Show good efficiency when the PSA that operating pressure is at least normal pressure is used for midget plant, but when being used for general 2 atmospheric pressure to 5 of pressure commonly used atmospheric pressure, the noise of pump and heating problem also have endurance issues just may occur.So it can not be used for the household electrical appliance of indoor use.Recently, having some to improve rate of recovery, to reduce the method for adsorption/desorption pressure simultaneously to greatest extent recommended, as U.S. Pat 5074,892; US6,010,55 and US6,506,234.But these methods are restricted owing to need to use high performance adsorbent and adsorbent to be difficult to regeneration.Also have, these methods are not paid attention to small-sized machine and productivity ratio, only be applicable to medical and and be not suitable on the small household appliances machine.In order to be applicable to small size home appliance, the technology that produces peak performance with low energy consumption is essential.
The VPSA of operation can ensure more quiet operation than PSA between atmospheric pressure and vacuum are pressed, but as mentioned above, and traditional construction method is because the multistep control of use complexity and valving and surge tank and can not reduce manufacturing cost.
Only, carry out absorption and desorb, use hair-dryer input concentrated gas by means of main vacuum pump at atmospheric pressure or the absolute VSA that operates below the atmospheric pressure.Like this, because it is little to put on the pressure reduction of adsorbent, this method has sizable advantage when being used to relate to the noise of vavuum pump and heating problem, but the formation of a machine needs two pumps at least, and this makes that this method is uneconomical.Must use high-performance adsorbent because productivity ratio is low when in addition, being applied on the small-sized machine.Also have, when the adsorbent bed more than 3 or 3 was arranged on the machine, valve control became complicated and is not suitable for packaged air-conditioner.
3. brief summary of the invention
In order to address this problem, the object of the present invention is to provide a kind of simple continuous production technology to boost productivity and simplified apparatus.That is, this technology can be used for small-sized gas concentration unit and produces a large amount of concentrated gas simultaneously.
The present invention also aims to provide a kind of use VPSA or VSA to have large-duty simple process, VPSA or VSA with compare at atmospheric pressure or the PSA that more than atmospheric pressure, operates, relative favourable aspect low noise, low heating and durability.
The object of the present invention is to provide and a kind ofly pay attention to the rate of recovery and productivity ratio and do not pay attention to the technology of the concentrated gas of production high concentration, the gas concentrator of a kind of VSA that only uses in atmospheric pressure or following operation especially is provided, and this gas concentrator uses high-performance adsorbent and has low noise and miniaturization.
The object of the present invention is to provide two adsorbent beds of a kind of use to produce continuously, the production changes in flow rate is few, and can control the gas concentration machine of concentrated gas concentration.
In order to realize aforesaid purpose of the present invention, embodiment according to the present invention provides a kind of by separate the gas concentration method of this specific gas behind difference of extra pressure on the adsorbent that specific gas is had selective absorption character, comprising:
The first step: the charging aperture by first adsorbent bed feeds raw gas mixture, the pressure of the pressure ratio raw gas mixture in this first adsorbent bed is low, in this first adsorbent bed, the component that the adsorbents adsorb adsorptivity is strong, internal pressure by reducing by second adsorbent bed adsorbed composition of desorb from this second adsorbent bed simultaneously, discharge the composition of adsorptivity relative mistake at the products export of this first adsorbent bed, produce concentrated gas, the microcapillary of the products export of the part of this concentrated gas by connecting this each adsorbent bed is input to this second adsorbent bed products export;
Second step: reduce pressure in this first adsorbent bed from charging aperture, the composition that desorb is adsorbed, by increase the pressure in second adsorbent bed from the charging aperture of this second adsorbent bed input raw gas mixture from charging aperture, the strong composition of absorption adsorptivity, there is barometric gradient between each products export of first and second adsorbent beds and the charging aperture in this process, the i.e. pressure height of the products export of pressure ratio second adsorbent bed of the products export of first adsorbent bed, so a part of product gas is input to the products export of second adsorbent bed from the products export of first adsorbent bed, produce continuously product gas, have in a flash the products export of first adsorbent bed and second adsorbent bed produce concentrated gas simultaneously in this step;
The 3rd step: the products export of first adsorbent bed and the barometric gradient between the second adsorbent bed products export reverse in second step, to such an extent as to it is opposite with the first step, the first adsorbent bed generation desorption process and the second adsorbent bed generation adsorption process, discharge concentrated gas from the products export of second adsorbent bed, the concentrated gas that will partly be produced from the products export of second adsorbent bed is input to the products export of first adsorbent bed simultaneously; With
The 4th step: opposite with second step, according to the barometric gradient in each adsorbent bed, part product gas is input to the products export of first adsorbent bed from the products export of second adsorbent bed, by importing raw gas mixture from charging aperture, increase the pressure in first adsorbent bed and carry out adsorption process from charging aperture, reduce the pressure in second adsorbent bed and desorption process takes place from charging aperture, also produce product gas in this process continuously, have in a flash the products export of first adsorbent bed and second adsorbent bed produce concentrated gas simultaneously in this step.
According to the present invention, under the situation of concentrater, mist is an air, and the composition that adsorptivity is strong is that the weak composition of nitrogen and adsorptivity is an oxygen.Also have, preferably, this adsorptive pressure is 1 to 2 air pressure to VPSA, is atmospheric pressure to VSA, and desorption pressures is pressed 200mmHg for the apparent vacuum of being measured by vacuum pump apparatus or (it is the following force value of 0 atmospheric pressure that apparent vacuum is pressed) more than the 200mmHg.
On the other hand, the invention provides a kind of device of concentrated gas, comprising:
The filter of impurity screening from raw gas mixture;
At least two adsorbent beds that comprise adsorbent;
The vacuum pump apparatus of additional vacuum pressure in adsorbent bed;
Alternately change the vacuum that applies vacuum pump apparatus and press and apply the valving in the path of mixture pressure;
The microcapillary that connects each adsorbent bed products export;
The product gas that makes the process products export is by the mobile check-valves of a direction;
Suck through behind the product gas of this check-valves this gas being ejected into the gas displacer of object space.
Preferably, between this check-valves and gas displacer, provide a controller, so that be controlled at the concentration and the flow of the product gas that the products export of adsorbent bed produces.This is because equipment according to the present invention is not limited to the applications in high concentration, and can be used for various occasions, from the lung ventilator of air-conditioner and 25～35% or higher,, need not adsorbent bed is carried out big change to 50% or higher water purifier as concentrater.
In addition, preferably, a mist control device is set, the combined amount of control mist and product gas, the concentration and the flow of the end product gas that control is connected with control device between check-valves and the gas displacer between this gas displacer and filter.Usually, the adsorbent that is included in the adsorbent bed can not be discharged impurity and moisture holomorphosis, so preferably reduce directly gas flow by adsorbent bed from life-span of adsorbent as far as possible.According to an example of the present invention, with these two control device make also not by the mist of adsorbent bed and the gas flow that mixes to reduce of the product gas by adsorbent bed by adsorbent bed be feasible.When these two control device were regulated the concentration of the given concentrated gas of answering use and flow, the controller between gas displacer and the filter was adjusted to the flow minimum that makes through adsorbent bed.
This vacuum pump apparatus and gas displacer can drive with same motor.And, the switch vacuum of preferred this check-valves is pressed and is set to 100mmHg or following apparent vacuum pressure, preferably be set to 50mmHg or following, so just can carry out second step and the 4th step by simple path conversion with the mist valve of adsorbent bed charging aperture.
4. description of drawings
Fig. 1 is four step of the standard schematic diagram of traditional PSA method.
Fig. 2 is three step of the standard schematic diagram of traditional RPSA method.
Fig. 3 is four step of a standard schematic diagram of the present invention.
Fig. 4 is according to the pressure-plotting in the adsorbent bed of the present invention.
Fig. 5 is the example according to gas concentration unit of the present invention.
Fig. 6 is the skeleton diagram according to the adsorbent bed pressure of gas concentration unit of the present invention.
Fig. 7 is the example of the gas concentration unit of traditional PSA technology.
5. DETAILED DESCRIPTION OF THE PREFERRED
Describe the present invention in detail below with reference to preferred embodiment.
Fig. 3 is the schematic diagram according to technology of the present invention.This technology was made of four steps of standard, and wherein Pl (P is low) refers to inhale relative low pressure and relative high pressure in one attached respectively with Ph (P height).
With reference to figure 3, first step is the adsorption process of the desorption process and the adsorbent bed 2 of adsorbent bed 1, angle from adsorbent bed 2, after mist flows into adsorbent bed 2, the composition that adsorptivity is strong is adsorbed agent absorption, the weak product gas of adsorptivity is discharged from by a products export simultaneously, and products export is a product gas outlet.Part product gas flows into and washs with relatively high pressure, high concentration the adsorbent of adsorbent bed 1 by the products export of adsorbent bed 1.The first step is to carry out 2 to 5 seconds for suitable in small-sized concentrater.Consider that the present invention is applicable to that VPSA and VSA and emphasis are to use an alap pressure, the mixture pressure that is input to adsorbent bed 1 by charging aperture to VPSA with 2 air pressure or following for suitable, and to absolute VSA, atmospheric pressure or the vacuum pressure of forcing down about tens mmHg than atmosphere are suitable.
Compare with the first step, second step occurred in the short relatively time period (being 2 seconds or following in midget plant).The input of the charging aperture mist by adsorbent bed 2 is interrupted, and vacuum pump apparatus starts and begins decompression, begins desorb thus.But, also there is barometric gradient in adsorbent bed 1 and the adsorbent bed 2, wherein the pressure of the products export of adsorbent bed 2 is higher than the pressure of the products export of adsorbent bed 1, so partial concentration gas flows to the products export of adsorbent bed 1 from the products export of adsorbent bed 2.At this moment, the continuous output concentrated gas of the products export of adsorbent bed 2.But, the pressure between the products export of adsorbent bed 2 and adsorbent bed 1 during near balance these two adsorbent beds produce concentrated gas simultaneously.Second step was proceeded after two adsorbent beds were produced concentrated gas simultaneously, and till the barometric gradient of each adsorbent bed products export reversed, gas was imported into the products export of adsorbent bed 2 from the products export of adsorbent bed 1 thus.
This part is one of principal character of the present invention, and it has utilized the barometric gradient in each adsorbent bed.Each adsorbent bed is produced concentrated gas by the on/off mode in the conventional art, when the production of the concentrated gas that interrupts an adsorbent bed and and another adsorbent bed when beginning to produce, the concentrated gas of production presents some fluctuations or discharge pressure reduction.And the present invention has relaxed this problem on sizable degree.
When the products export pressure of the products export pressure ratio adsorbent bed 2 of adsorbent bed 1 was high, the 3rd step carried out in the mode opposite with the first step.Promptly when the reversal of direction of flow of the concentrated gas between each products export of the first step, the products export adverse current of a part of product from the products export of adsorbent bed 1 to adsorbent bed 2, product gas is discharged continuously.Like this, adsorbent bed 2 carries out desorb, and adsorbent bed 1 adsorbs.From the angle of adsorbent bed 1, mist is continuously introduced to adsorbent bed 1, and in adsorbent bed 1, the composition that adsorptivity is strong is adsorbed agent absorption, and the weak product gas of adsorptivity is discharged by products export, and products export is a product gas outlet.Part in the product gas flows into and washs with relatively high pressure, high concentration the adsorbent of adsorbent bed 2 by the products export of adsorbent bed 1.
The same with in second step, the 4th step was translate phase, in this step, adsorbed and desorb reverses between each adsorbent bed.The part of product gas still is transfused to the direction identical with the 3rd step because of the barometric gradient in each adsorbent bed, that is, a part of concentrated gas is input to the products export of adsorbent bed 2 from the products export of adsorbent bed 1.At this moment, product gas is discharged continuously.Like this, the input of the mist of the charging aperture by adsorbent bed 1 is interrupted, and vacuum pump apparatus starts and begins decompression, begins desorb thus.On the other hand, by the charging aperture input mist of adsorbent bed 2, adsorbent bed 2 increases pressure, begins absorption thus.When in the 4th step, also having adsorbent bed 1 and 2 to produce concentrated gas simultaneously.
From second go on foot the 3rd the step and from the 4th the step be transformed into the transfer process of the first step the identical process of mobile process of the pressure of each adsorbent bed products export and concentrated gas.
Each adsorbent bed pressure below is described in detail by the variation of time as shown in Figure 6 in each step.
The mobile pressure differential of having utilized between each adsorbent bed products export of the concentrated gas in each step between the adsorbent bed.Though do not need one to adjust equipment or the valve that concentrated gas flows specially, in order to produce concentrated gas reposefully, the hole of using suitably design between each products export is for well.
At the pressure of above-mentioned each charging aperture, use vacuum pump apparatus and gas compressing apparatus, to VSA, pressing tens mmHg with apparent vacuum serve as suitable to barometric pressure range, to VPSA, with 2 air pressure or following serve as suitable.The pressure of products export is pressed in 300mmHg to 1.8 air pressure range in apparent vacuum usually and is moved by the discharge method decision of the pressure and the product of charging aperture.The discharge pressure of concentrated gas is by determining at that employed gas displacer.When the pressure by input gas determines,, serve as suitable with 1.8 air pressure or following scope as in VPSA technology.Use VSA technology in embodiment according to the present invention---during by vacuum pump apparatus and gas displacer input concentrated gas, the pressure that equals mist with adsorptive pressure is for well.During oxygen in the separation of air with atmospheric pressure for well.Desorption pressures is to be pressed by the 200mmHg of vacuum pump apparatus decision or above apparent vacuum to well.The pressure of products export is to force down tens mmHg to 300mmHg pressure limits for good than atmosphere.
In addition because the separation of oxygen is mainly considered in application of the present invention, so the admixture of gas of input with air for well.For oxygen concentration, when the strong composition of adsorptivity is nitrogen and composition a little less than the adsorptivity when being oxygen, product gas is an oxygen and desorption gas is a nitrogen.Certainly, can carry out the separation of variety classes gas according to the character of the contained adsorbent of adsorbent bed and concentrate.According to the present invention, can select suitable adsorbent according to the gaseous species of being produced.
Fig. 3 is according to an example of the present invention, and is different with Fig. 1, and each step among Fig. 3 all produces and can produce continuously.Also have, the product of products export flows and is stably and its amplitude of fluctuation is very little.Each step of a circulation finished rapidly in several seconds.Each step can be at 3 seconds to finish.As being used for the miniature bed of household small-size concentrater, whole circulation can be finished in 10 seconds.
In fact, art production process shown in Figure 1 is discontinuous carrying out and since each the step change of production big, so need surge tank (US6,663,691, JP-A-4-505448,4-222613).Selectively, being extended to many bed process changes and changes in flow rate to reduce pressure.This moment, the formation of valve became complicated, must use to have the rotary valve that the path is formed at the rotating disk of motor and adsorb and desorb to control.On the other hand, among Fig. 3, run through whole steps, concentrated gas is produced continuously.And product gas is stably at the mobile of products export.So it is very little only just can to keep the discharge pressure fluctuation and the changes in flow rate of concentrated gas with two adsorbent beds, and does not need additional surge tank.
Fig. 4 is the pressure-plotting by length in the adsorbent bed 1.As shown in Figure 4 and RPSA similar, in adsorbent bed, use the granule adsorbent usually to manifest barometric gradient.Adsorbent bed is filled with as far as possible little adsorbent.Because each step carried out in the very short time, so there is barometric gradient between the entrance and exit.Two bigger barometric gradients appeared at for second step and the 4th step, and this barometric gradient continues till the products export pressure of adsorbent bed 1 and 2 reaches balance.When second step when carrying out forward, the products export pressure of adsorbent bed 1 increases the pressure greater than the products export of adsorbent bed 2, thus the products export from the products export adverse current of adsorbent bed 1 to adsorbent bed 2, as the 3rd step take place, produce concentrated gas.
Being used for desorption pressures according to this optimal process of the present invention is VPSA and the VSA that vacuum is pressed, though it also is used on the PSA of the above operation of normal pressure.For each step produces continuously, it is more suitably that device as shown in Figure 5 is used for VSA, in this device independent pump that is used to discharge product gas be used to reduce the product changes in flow rate and can be under low pressure difference quiet the operation.This is because the objective of the invention is to use on small oxygen device thickener.For peace and quiet operation and large-scale production, should use the high-performance adsorbent of nearest exploitation, like this, desorption pressures is arranged on vacuum and depresses to good.As everyone knows, making adsorbent long-term regeneration with the washing of the oxygen of simple atmospheric pressure wash conditions and relative high concentration is suitable difficulty.Therefore, technology of the present invention between atmospheric pressure or above and vacuum are pressed operation or as Fig. 5 fully atmospheric pressure or following operating to.Fig. 5 is for using the example at the gas concentration unit of atmospheric pressure operation with two adsorbent beds of above-mentioned technology.
As shown in Figure 5, use the gas concentration unit of technology of the present invention to comprise: the filter 3 of impurity screening from mist, inside comprises the adsorbent bed 1 of adsorbent, 1 ', to this adsorbent bed 1, add the vacuum pump apparatus 4 that vacuum is pressed on 1 ', to adsorbent bed 1,1 ' alternately applies the pressure of the mist that passes through filter 3 and the valving 2 of pressing according to the vacuum of vacuum pump apparatus 4, make the part of the product gas of in an adsorbent bed, producing flow into the microcapillary 5 of another adsorbent bed, the check-valves 6 that product gas is flowed by a direction, 6 ' and make final concentrated gas be discharged into the gas displacer 7 in desired space, further comprise the controller 8 of controlling product gas flow and concentration, 9.
This gas displacer 7 can be a kind of vavuum pump, and has and be enough to by controller 8 and check-valves 6,6 ' suck concentrated gas and its vacuum that ejects is pressed from adsorbent bed 1,1 ' products export.Therefore, check-valves 6,6 ' switch vacuum are pressed with low to well.Based on this kind reason, check-valves does not use being shaped as merely of spring to constitute with rubber.Under situation about constituting with spring with the very low small spring of elasticity for well.Gas displacer 7 can be provided with an independently vacuum pump apparatus or use two vavuum pump heads to be installed on the motor of vacuum pump apparatus 4, and they are driven respectively and resemble a vavuum pump.Valving 2 magnetic valve, at this moment obvious other controllers that need of comprising as be known in the art.Can use the same rotary valve that the path is formed at the rotating disk of motor that has with valving 2.
Known to those skilled in the art, the circuit board control magnetic valve that rotary valve need not be other only just can be realized the switch transition of passage fully with Mechanical Driven.
This microcapillary 5 connects each adsorbent bed 1,1 ' products export, preferably includes the hole that some have a predefined flow resistance.It can be directly connected to adsorbent bed 1,1 ' opening also can use other hole parts.
With of the present invention and method or install relevant content, the prior art relevant with RPSA and with VSA relevant prior art is all in this citation as a reference.
The operating process of the device of Fig. 5 is as follows: at first, the first step applies a vacuum pressure by vacuum pump apparatus 4 to adsorbent bed 1 through valving 2, charging aperture from mist, the inside of adsorbent bed is depressurized, and reaches this vacuum and presses, and adsorbent bed carries out desorption process thus.At this point, the part of the concentrated gas that another adsorbent bed 1 ' lining produces is washed by the products export inflow of adsorbent bed 1.Gas displacer 7 sucks at the concentrated gas of adsorbent bed 1 ' interior production and is ejected into the space of requirement.In second step, the pressure of the mixed gas of mist of process filter 3 and valving 2 and a difference that interior vacuum is pressed are passed through inlet suction adsorbent bed 1, and the pressure in this process bed of process begins rising.Since the pressure of the products export of adsorbent bed 1 still than adsorbent bed 1 ' the pressure of products export low, a part of product gas is inhaled into adsorbent bed 1 adsorbent bed 1 ' continuations production simultaneously.Adsorbent bed 1,1 ' products export pressure equate before and afterwards, attached bed 1,1 ' is simultaneously produced.Here, gas displacer 7 should have be enough to overcome check-valves 6,6 ' resistance from adsorbent bed 1,1 ' products export suck the suction of product gas.So check-valves 6,6 ' should have fully low open/close pressure as mentioned above.After this, carry out the 3rd step of production in adsorbent bed 1.Opposite with the first step, adsorbent bed 1 is produced, adsorbent bed 1 ' carry out desorption process and washing process.The 4th step is opposite with second step, adsorbent bed 1,1 in the 4th step ' mutual conversion role each other.
8 controls of this controller by adsorbent bed 1,1 ' the flow and the concentration of product gas, controller 9 suitably mixes the gas through the mist of filter 3 and adsorbent bed 1,1 ' produced, and controls the flow and the concentration of the concentrated gas of displacer 7 injections.Can use a variable flow control valve and fixing hole fixed concentration and flow to obtain final concentrated gas.The adsorbent of adsorbent bed 1,1 ' comprise generally is difficult to removal of contamination and moisture holomorphosis, so the life-span of considering adsorbent is to reduce the gas flow that directly passes through adsorbent bed 1,1 ' for well as far as possible.Embodiment according to the present invention can be mixed not mist by adsorbent bed and the product gas by adsorbent bed with controller 8 and 9 and be reduced gas flow by adsorbent bed.When the flow of given certain applications and concentration, controller 8 is arranged on the initial stage design point, adjust controller 9 then and make its definite object concentration and flow, simultaneously with checking that the method whether flow reaches aimed concn fully minimizes the gas flow by adsorbent bed.In case this adjustment is finished, realize fixing aimed concn and flow with fixing hole as mentioned above.
As mentioned above, the suction pressure of check-valves 6,6 ' switch pressure and gas displacer 7 is very important in operating process.If check-valves 6,6 ' switch pressure are excessive, the pressure of adsorbent bed 1,1 ' products export may all be closed two check-valves 6,6 '.So check-valves 6,6 ' switch vacuum are pressed with low to well.Usually it is in 100mmHg or following apparent vacuum pressure scope.Gas displacer 7 is devices that concentrated gas are ejected into desired space, and whether its discharge pressure is critical being determined by the occasion that will use.Usually, its suction greatly influences the performance of device.Go for method of the present invention fully with controller 8 when having sufficient vacuum and press as piston or membrane pump etc.On the other hand, when the hair-dryer that uses bargain-hunting power or with the airlift pump of electromagnet vibration rubber slab to pet fish with fish jar on during input air, check-valves 6,6 ' switch pressure are very important.So check-valves 6,6 ' generally has 100mmHg or following apparent switch vacuum is pressed, preferably with 50mmHg or following, even the gas displacer 7 that uses has 200mmHg or following bargain-hunting power so that method of the present invention can reach fully.In this case, only use check-valves 6,6 ' switch pressure also concentration and flow can be adjusted to a certain degree, so, can omit controller 8, only regulate desired concentration and flows with a controller 9.
Fig. 6 is that adsorbent bed 1,1 ' pressure change skeleton diagram, and the pressure of mist is 1 atmospheric pressure among the figure.In Fig. 6, suppose that A and B are respectively the mist charging aperture of adsorbent bed 1 and the pressure history of products export, C and D be adsorbent bed 1 ' charging aperture and during the pressure history of products export, when the angle of adsorbent bed 1 is seen, t1 represents desorption process, and t2 represents adsorption process.In addition, X is the suction pressure of the charging aperture of the device gas displacer 7 of supply concentrated gas.Through with the pressure ratio that puts on adsorbent bed 1,1 ' products export, by controller 8 and the check-valves 6,6 ' as resistance gauge, if the pressure B and the D of adsorbent bed 1,1 ' products export are big greater than X, displacer produces product gas.Fig. 6 is the embodiment with continuous production capacity, and wherein the t3 in second step or the 4th step is the state of the pressure of adsorbent bed 1,1 ' products export greater than pressure X, so represent two adsorbent beds 1, the 1 ' process of producing simultaneously.Pressure X is set to force down 100 to 300mmHg for good than atmosphere.If pressure X is low, then there is a kind of trend, i.e. the expanded range of producing product gas simultaneously at the products export of adsorbent bed 1 and adsorbent bed 2, and the oxygen concentration of product gas is low.Therefore, pressure X is configured such that the fluctuation range of concentration and flow is minimised as in given aimed concn and flow.
When method of the present invention was applied to aforesaid VSA system, the length that the carrying out time in second step and the 4th step can be by adjusting adsorbent bed and the size of diameter and adsorber particles be adjusted the resistance that sucks gas, so that the barometric gradient variation.The adsorbent that adsorbent bed uses can have been bought on market.Usually use 5A-zeolite (zeolites in 5 angstrom unit apertures) during from air separation oxygen.About adsorbent bed, the prior art relevant with this RPSA fully quoted as a reference at this.In addition, suction pressure that can be by adjusting gas displacer 7 and check-valves 6,6 ' switch pressure adjusted for second step and the 4th step.So adjust the control of concentration and flow very importantly, and preferably use independently controller 8,9 to finish so that gas displacer 7 possesses sufficient suction pressure, check-valves 6,6 ' has alap switch pressure.
Use the check-valves 6,6 ' of switch pressure very low (apparent vacuum is pressed 50mmHg or following), this method just can realize for second step and the 4th step by simple valve stream conversion, need not complicated valve control.Promptly, because the first step and the 4th step are identical with the desorb path direction in adsorbent bed 1,1 ' charging aperture absorption, second step is also identical with the 3rd step, so only make the stream conversion just form adsorbent bed 1,1 ' barometric gradient naturally at adsorbent bed 1,1 ' charging aperture, so finished this four steps by simple valve ON/OFF.Certainly, according to given technology by control be arranged on adsorbent bed 1, each valve of 1 ' is carried out this method and be will be readily apparent to persons skilled in the art.Therefore, use two general solenoid valves can constitute valving 2 simply, or use and to have the rotary valve that the path is formed at the rotating disk of motor, these all are known to those skilled in the art.Use aforesaidly have check-valves that the low switch vacuum presses 6,6 ' time, just can carry out method of the present invention by the control of simple valve, or even in the hair-dryer or foaming pump that use apparent vacuum pressure 200mmHg or following low suction pressure.
According to the present invention,, can produce a large amount of concentrated gas effectively by using the technology of main consideration productivity.Utilize technology of the present invention, small-sized gas concentration machine can be produced a large amount of concentrated gas, in particular for placing on the concentrater in the household electrical appliance of family expenses, or is used for the portable oxygen thickener, can constitute small-sized, cheap and high efficiency device.When being used to use the system of VSA technology, the present invention freely controls the flow and the concentration of concentrated gas and makes the adsorbent lifetime by simplifying parts, overcomes the noise of conventional small gas concentrator and endurance issues simultaneously and realizes economy.
Claims (3)
- Thereby 1, a kind of gas concentration method by the difference separation specific gas of exerting pressure to the adsorbent that gas is had selective adsorption capacity comprises:The first step: the charging aperture by first adsorbent bed feeds raw gas mixture, the pressure of the pressure ratio raw gas mixture in this first adsorbent bed is low, in this first adsorbent bed, the component that the adsorbents adsorb adsorptivity is strong, internal pressure by reducing by second adsorbent bed adsorbed composition of desorb from this second adsorbent bed simultaneously, discharge the composition of adsorptivity relative mistake at the products export of this first adsorbent bed, produce concentrated gas, the microcapillary of the products export of the part of this concentrated gas by connecting this each adsorbent bed is input to this second adsorbent bed products export;Second step: reduce pressure in this first adsorbent bed from charging aperture, the composition that desorb is adsorbed, by increase the pressure in second adsorbent bed from the charging aperture of this second adsorbent bed input raw gas mixture from charging aperture, the strong composition of absorption adsorptivity, there is barometric gradient between each products export of first and second adsorbent beds and the charging aperture in this process, the i.e. pressure height of the products export of pressure ratio second adsorbent bed of the products export of first adsorbent bed, so a part of product gas is input to the products export of second adsorbent bed from the products export of first adsorbent bed, produce continuously product gas, have in a flash the products export of first adsorbent bed and second adsorbent bed produce concentrated gas simultaneously in this step;The 3rd step: the products export of first adsorbent bed and the barometric gradient between the second adsorbent bed products export reverse in second step, to such an extent as to it is opposite with the first step, the first adsorbent bed generation desorption process and the second adsorbent bed generation adsorption process, discharge concentrated gas from the products export of second adsorbent bed, the concentrated gas that will partly be produced from the products export of second adsorbent bed is input to the products export of first adsorbent bed simultaneously; WithThe 4th step: opposite with second step, according to the barometric gradient in each adsorbent bed, part product gas is input to the products export of first adsorbent bed from the products export of second adsorbent bed, by importing raw gas mixture from charging aperture, increase the pressure in first adsorbent bed and carry out adsorption process from charging aperture, reduce the pressure in second adsorbent bed and desorption process takes place from charging aperture, also produce product gas in this process continuously, have in a flash the products export of first adsorbent bed and second adsorbent bed produce concentrated gas simultaneously in this step.
- 2, method according to claim 1, wherein this mist is an air, the component that this adsorptivity is strong is that the weak component of nitrogen and this adsorptivity is an oxygen.
- 3, method according to claim 1 and 2, wherein this adsorptive pressure is an atmospheric pressure, this desorption pressures is to be pressed by the apparent vacuum that vacuum pump apparatus is measured.
Applications Claiming Priority (6)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| KR1020030010176 | 2003-02-18 | ||
| KR1020030010178 | 2003-02-18 | ||
| KR10-2003-0010176A KR100476161B1 (en) | 2003-02-18 | 2003-02-18 | Gas concentrator |
| KR1020030028407 | 2003-05-03 | ||
| KR1020030029102 | 2003-05-07 | ||
| KR1020030051275 | 2003-07-25 |
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| CN1309455C true CN1309455C (en) | 2007-04-11 |
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| CNB2004800000114A Expired - Lifetime CN1309455C (en) | 2003-02-18 | 2004-02-16 | Gas concentration method and its apparatus |
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| KR (1) | KR100476161B1 (en) |
| CN (1) | CN1309455C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101687134B (en) * | 2007-04-20 | 2013-12-18 | 英瓦卡尔公司 | Product gas concentrator and method associated therewith |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100520904B1 (en) * | 2005-02-16 | 2005-10-11 | (주)엘티오투 | The true form structure for oxygen occurrence equipment |
| US8940081B2 (en) * | 2010-01-26 | 2015-01-27 | Osaka Gas Co., Ltd. | Combustible gas enrichment apparatus |
| EP2822671B1 (en) | 2012-03-09 | 2018-10-03 | Invacare Corporation | System and method for concentrating gas by adsorption |
| TWI771584B (en) * | 2019-05-13 | 2022-07-21 | 純萃材料股份有限公司 | Adsorption apparatus and adsorption method |
| FR3096278B1 (en) * | 2019-05-23 | 2021-09-10 | Air Liquide | Method of adjusting an oxygen production unit by comparing the differential pressures characteristic of the different adsorbers |
| US11915570B2 (en) | 2020-07-16 | 2024-02-27 | Ventec Life Systems, Inc. | System and method for concentrating gas |
| US11931689B2 (en) | 2020-07-16 | 2024-03-19 | Ventec Life Systems, Inc. | System and method for concentrating gas |
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| EP0589406A2 (en) * | 1992-09-23 | 1994-03-30 | Air Products And Chemicals, Inc. | 02 VSA process with low 02 capacity adsorbents |
| CN1148517A (en) * | 1995-05-19 | 1997-04-30 | 乔治·克劳德方法的研究开发空气股份有限公司 | Device and process for separating gases by adsorption |
| CN1284473A (en) * | 1999-08-13 | 2001-02-21 | 普拉塞尔技术有限公司 | Pressure rotating adsorption method for production of hydrogen |
| US6406520B1 (en) * | 1999-07-22 | 2002-06-18 | L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude | Adsorbent having improved selectivity for the separation of gases |
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2003
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| EP0589406A2 (en) * | 1992-09-23 | 1994-03-30 | Air Products And Chemicals, Inc. | 02 VSA process with low 02 capacity adsorbents |
| CN1148517A (en) * | 1995-05-19 | 1997-04-30 | 乔治·克劳德方法的研究开发空气股份有限公司 | Device and process for separating gases by adsorption |
| US6406520B1 (en) * | 1999-07-22 | 2002-06-18 | L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude | Adsorbent having improved selectivity for the separation of gases |
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| CN101687134B (en) * | 2007-04-20 | 2013-12-18 | 英瓦卡尔公司 | Product gas concentrator and method associated therewith |
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| Publication number | Publication date |
|---|---|
| KR100476161B1 (en) | 2005-03-15 |
| KR20040074421A (en) | 2004-08-25 |
| CN1697681A (en) | 2005-11-16 |
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