CN1010378B - Improved differential pressure adsorption process and equipment - Google Patents
Improved differential pressure adsorption process and equipmentInfo
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- CN1010378B CN1010378B CN 86102699 CN86102699A CN1010378B CN 1010378 B CN1010378 B CN 1010378B CN 86102699 CN86102699 CN 86102699 CN 86102699 A CN86102699 A CN 86102699A CN 1010378 B CN1010378 B CN 1010378B
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Abstract
In a variable-pressure adsorption technique applied to the separation of air and other kinds of gas, the cycling time is shortened by introducing simultaneous operation steps, a cocurrent-flow pressure reducing step is started from high adsorption pressure intensity so that the extracted gas is simultaneously used for balancing pressure intensity and is used as sweeping gas. Cocurrent-flow pressure reduction is carried out under intermediate pressure intensity, and counter-flow pressure reduction is simultaneously carried out on the other end of a bed layer so that the pressure is reduced to low desorption pressure intensity.
Description
The present invention relates in pressure swing adsorption system, carry out the purification of gas.Present invention is specifically related to and to make operating characteristics better in the circulation and the improvement of system aspects.
Transformation absorption (PSA) process is at least one component in separation and the purification raw gas mixture, and a kind of technology of commercial needs is provided.This raw gas mixture is made up of above-mentioned component and at least one alternative adsorbed components, under higher absorption pressure, adsorbent bed absorption, then, adsorbent bed pressure drop to lower desorption pressure, is separated sucking-off by the selectivity adsorbed components.Available Wagner patent (U.S. 3430418) illustrates that the pressure-swing absorption process of carrying out, this process have 4 beds at least in multibed system.In this patent, narrated the circulation pressure-swing absorption process of generally all knowing, the cyclic process of each bed all comprises the sequence of operations step: (1) is under higher absorption pressure, products export extraction product gas from bed: (2) cocurrent flow is decompressed to intermediate pressure, gas in the products export extraction bed space of above-mentioned bed, (3) countercurrent depressurization is to lower desorption pressure; (4) purge and (5) repressurize.Gas during cocurrent flow decompression in the bed space of extraction is usually used in pressure equilibrium and as the purge gas that is in than the bed under the low pressure.
In above-mentioned said various pressure-swing absorption processes with four or more bed system, design separation and recovery and other separation of gaseous mixture that three bed systems are used for air usually.This system is based on the cumulative adsorption step of pressure of narration in the McCombs patent (U.S. 3,738087).In the embodiment therein, air is added adsorbent bed, make the bed supercharging, nitrogen is wherein adsorbed by selectivity, and simultaneously with certain speed, from the products export extraction oxygen wherein of bed, bed just increases to higher absorption pressure like this.The pressure-swing absorption process that has the cumulative adsorption step of pressure comprises: the cumulative adsorption step of (1) above-mentioned pressure; (2) cocurrent flow is decompressed to intermediate pressure, the gas in the products export extraction bed space of bed; (3) countercurrent depressurization is to lower desorption pressure; (4) purge and (5) decompression.In the above-described embodiment, in the order of pressure equilibrium-generation purge gas-pressure equilibrium, will add other bed of system at the gas in the bed space of extraction during the cocurrent flow decompression.The isobaric adsorption step that the latter's circulation is adopted the Wagner circulation there is no need.So just make bed have more time to regenerate, just in certain circulation timei, have more time to carry out countercurrent depressurization and purging, especially for short system of the operation cycle total time of design, it can obtain higher production capacity, the rate of recovery and (or) purity.
Use three such bed system.Each bed is equipped with commercial 13X, and 8 * 12 column molecular sieves carry out air separation, and the rate of recovery that obtains oxygen is 48%, and production capacity (BSF) is 4000 pound 13X molecular sieves/ton oxygen sky (TPD).The product oxygen that the above-mentioned rate of recovery is defined as recovery accounts for the percentage or the volume fraction of the oxygen in the raw air, and above-mentioned production capacity (BSF) is defined as and produces the one ton of needed molecular sieve pound of oxygen number every day.The numerical value of the above-described rate of recovery and production capacity is by one three bed system, and the global cycle cycle is when being 180 seconds, the highest pressure of the raw air of acquisition inlet be the 2.8[kilogram/(centimetre)
2] (gauge pressure), the product gas back pressure be the 1.4[kilogram/(centimetre)
2] (gauge pressure).
Three bed systems of standard although it is so can satisfy various commercial uses, but still wish to improve technically the rate of recovery and the production capacity of product.But, run into a lot of difficulties for realizing these purposes.For example, reduce (even production capacity increase), must reduce total cycle time, make it to be lower than above-mentioned 180 seconds for the BSF value is had significantly than above-mentioned standard three bed systems., reduce individual steps, just reduce purging and time of pressure equilibrium step, be subjected to the restriction of gas velocity and bed fluidization scope or be subjected to the restriction of spendable cycle performance standard.Because these restrictions are arranged,, be impossible reduce total circulation timei significantly only by reducing the time of indivedual circulation steps.On the other hand, for four bed systems of standard, by using the relevant standard cycle technology of said system, introduce the 5th bed the production capacity of single bed is increased, for certain application scenario, this can cause increasing total circulation timei and BSF value.The increase of BSF value can damage owing to increased the potential production capacity that the bed number increases in pressure swing adsorption system.On the other hand, in the transformation absorption, the size restrictions of oxygen absorbent bed the maximum productivity of single transformation absorption series.Therefore, need exploitation to reduce the technology of BSF value, adsorb the scope of the maximum productivity of series to increase this single transformation.Thereby, still be necessary to improve pressure swing adsorption technically, make the BSF value reduce, the production capacity of single transformation absorption series increases.These improvement can help reducing total cycle time, but still have time enough to finish each circulation step, are unlikely to reduce the purity and the rate of recovery of product.
Therefore, the purpose of this invention is to provide an improved pressure-swing absorption process and system.
Another object of the present invention provides a pressure-swing absorption process and system and be used for separating and reclaiming oxygen from air.
A further object of the invention provides a pressure-swing absorption process and system and makes and reduce to minimum total circulation timei, but still has time enough to finish each independent circulation step, and is unlikely to reduce the purity and the rate of recovery of product.
The present invention who below is described in detail for the purpose of these and other, particularly points out characteristics of the present invention just in the appended claims.
Pressure-swing absorption process of the present invention and system have advantageously adopted circulation step novel the time, make total cycle time reduce, and the rate of recovery of product increases, and the BSF value reduces.Independently provide the required time of step of purge gas to wish than the purge step weak point, in implementing the short total cycle time of the present invention's permission, wherein the time of countercurrent depressurization and purging can enough make the bed realization regenerate fully.
By the pressure-swing absorption process in the Wagner patent of narration more than circulation step is introduced simultaneously, realize the present invention's purpose.So-called circulation step simultaneously is meant in global cycle and reduces pressure the stage relevant with countercurrent depressurization steps with cocurrent flow.These while circulation steps reduce total cycle time, and the BSF value is reduced, even the production capacity of adsorbent increases.Implement when of the present invention, can be under total cycle time be reduced to minimum situation, the bed production capacity that is strengthened, and can not reduce the purity or the rate of recovery of product.Compare with industrial three pressure-swing absorption processes of the standard of above narration and the result of system, found that product recovery rate of the present invention has had significant improvement actually.
Should be noted that, a suitable embodiment of the present invention has adopted the strong adsorption step of constant voltage in the above-mentioned Wagner circulation, be that adsorption bed is under the higher absorption pressure conditions of maintenance, unstrpped gas is passed through bed, the component that easily is adsorbed optionally is adsorbed, simultaneously, the component that is adsorbed from the products export extraction difficulty of bed is as product, can access less BSF value through the strong sorption cycle of the improved this constant voltage of the present invention, thereby, concerning certain production capacity and purity, this circulation makes uniserial production capacity higher, and the charge weight of adsorbent is reduced.Therefore, it will be understood that below narration is the improvement of the present invention to the above-mentioned total operation cycle of quoting of Wagner.
The present invention can very advantageously be applied to have at least four adsorbent bed many bed pressure swing adsorption systems.In some application scenario, four adsorption systems are more closed the symbol needs.In other occasions, five, six or seven adsorption systems also are desirable.Although can realize the pressure swing adsorption system of eight or more a plurality of beds, use usually two four bed systems or similarly system replace having the single-row system of more bed numbers more favourable.In such multibed system, in any moment of cyclic process, unstripped gas will pass through more than one bed, and this is understandable, and for example, when operating such system, in any given time, unstripped gas is usually by at least two beds.As traditional practice, pressure-swing absorption process wishes to adopt two, three or more pressure equilibrium step, therebetween, cocurrent flow depressed gas from a bed extraction under High Voltage is used to make the another one bed part supercharging that is at first than low pressure, also is used as the purge gas that is in than the bed of low pressure.Therefore, the present invention can be used for multiple operation cycle, for example, comprises the circulation of five or more beds.In total operation cycle of transformation absorption, at any given time, wherein there are two beds to be in adsorption step with partly overlapping order, persons skilled in the art will be understood that, can adopt other various pressure-swing absorption processes and system, so that obtain superiority of the present invention with suitable transformation sorption cycle.
The following table I can be used for illustrating how to implement the present invention.It is for one four bed system embodiment of the present invention.
For each bed, A is illustrated in component that the adsorption step under the higher absorption pressure is adsorbed from the products export extraction difficulty of bed as product in the last table, PP represents the cocurrent flow depressurization steps, during this period, above-mentioned bed is decompressed to intermediate pressure from higher intermediate pressure, gas in the products export extraction bed space of bed is as the purge gas that is in another bed under the low desorption pressure; P represents to be in the purge step under the low desorption pressure, during this period, gas in the bed space of another bed extraction directly feeds the above-mentioned bed that is in purge step, and the time of above-mentioned purge step is more longer than the cocurrent flow depressurization steps PP that produces purge gas; R represents to be pressurized to the pressure increase step of higher absorption pressure; E1/PP represents one of them novel step of the present invention, cocurrent flow depressurization steps just, in this step, be decompressed to higher intermediate pressure from higher absorption pressure, another bed in the gas feeding system in the bed space of extraction, this bed positive part is pressurized to above-mentioned higher intermediate pressure, also feeds simultaneously to be in than other second bed that hangs down desorption pressure as purge gas; E2/BD represents another novel step of the present invention, in this step, further carry out the cocurrent flow decompression, from middle pressure drop to lower intermediate pressure, gas in the more bed of the products export extraction space of bed, another bed with in this gas feeding system makes each other under lower intermediate pressure, reach pressure equilibrium, and above-mentioned bed carries out countercurrent depressurization from the unstripped gas inlet extraction gas of bed simultaneously.BD in the above-mentioned E2/BD step partly is that countercurrent depressurization partly is performed until and makes bed be decompressed to lower desorption pressure, finishes till the above-mentioned pressure equilibrium.In the process of the embodiment of above-mentioned table I explanation, in four bed systems,, only there is a bed to be in adsorption step as can be seen in any preset time of a cycle period.Therefore adopted two pressure equilibrium steps, just above-mentioned E1/PP and E2/BD step and with they corresponding E2/ and E1 step, title (412) E1/PP-E2/BD in the table I is meant global cycle, here 4 expression bed numbers; 1 is illustrated in the bed number that is in adsorption process any preset time; The direct pressure equilibrium number of steps of 2 expressions; E1/PP-E2/BD represents two novel features of the present invention.The pressure-swing absorption process has here adopted two while operating procedures of above narration, thereby has obtained the pointed superiority of the present invention of this paper.
In the operation cycle that in the table I, illustrates, for example, bed 1 carries out the cocurrent flow decompression at E1/PP step bed, will be from the gas in the bed space of the products export extraction of bed, feed bed 3, under higher intermediate pressure, carry out pressure equilibrium, meanwhile, feed the initial period of bed 4 as the purge step of this bed.Proceed the cocurrent flow depressurization steps of bed 1, the gas in the bed space of extraction feeds bed 4 as purge gas during this period, and bed 1 further is decompressed to intermediate pressure.And then carry out the E2/BD step, remaining gas in the products export extraction bed space of bed 1, the bed cocurrent flow is decompressed to lower intermediate pressure, and above-mentioned gas feeds bed 4, under above-mentioned lower intermediate pressure, carries out pressure equilibrium.From the unstripped gas inlet extraction gas of bed 1, make bed 1 countercurrent depressurization simultaneously.The BD stage in the E2/BD step is performed until and makes the bed 1 that reducing pressure and just at the bed 4 of supercharging, under above-mentioned lower intermediate pressure, reach till the pressure equilibrium.From this example as can be seen, the E2 step is represented the part supercharging of bed, promptly by the gas in the bed space is directly added bed, make bed increase to lower intermediate pressure from lower desorption pressure, above-mentioned gas is that a bed is in the E2/BD step and carries out cocurrent flow when decompression extraction, by with the pressure equilibrium of the above-mentioned bed of supercharging partly, make this bed be decompressed to above-mentioned lower intermediate pressure, and above-mentioned bed increase to above-mentioned lower intermediate pressure from lower desorption pressure from middle pressure.Equally, E1 represents by the gas in the bed space is directly fed bed, makes it further partly be pressurized to higher intermediate pressure.Above-mentioned gas is extraction from the bed of the cocurrent flow decompression that is in the E1/PP step, by with the pressure equilibrium of the above-mentioned bed of supercharging partly, make this bed be decompressed to higher intermediate pressure, and above-mentioned bed increase to higher intermediate pressure from lower intermediate pressure from higher absorption pressure.
When the operation cycle of the present invention that table is represented in the I is applied to actual commercial air separation operation, higher absorption pressure be the 28[kilogram/(centimetre)
2] operate each bed under (gauge pressure), can effectively utilize 160 seconds total cycle times.The BSF value of industrial 13X8 * 12 column type adsorbent of molecular sieve is 3000 pound 13X/ ton product oxygen (purity is 90%) day, and the rate of recovery of product oxygen is 53%, in contrast, same 28[kilogram/(centimetre)
2] operate under the absorption pressure of (gauge pressure), use 5A, 8 * 12 column type molecular sieves, production purity is 90% oxygen product, and the total cycle time of four Wagner circulatory system needs is 240 seconds, and the BSF value is higher, be 6000 pound 5A/ ton oxygen product skies, just production capacity is lower.
Adopted in another gratifying embodiment of the present invention five adsorbent bed, at any given time, wherein there are two beds to be in adsorption step, the same with the embodiment of above explanation, two pressure equilibrium steps and E1/PP of the present invention and E2/BD step have been adopted, therefore in the following table II, claim this cyclic process to be (522) E1/PP-E2/BD circulation.
In the cyclic process of table II, the represented meaning of A, E1/PP, PP, E2/BD, P, E2, E1 and R and the embodiment in showing I is identical.Implement above-mentioned (522) E1/PP-E2/BD circulation, separable air, the higher absorption pressure of employing be the 28[kilogram/(centimetre)
2] (gauge pressure), with same industrial 13X, 8 * 12 column type adsorbent of molecular sieve, be 200 seconds total circulation timei, the oxygen product purity that obtains is 90%, the BSF value is about 3800 pound 13X/ ton oxygen product skies, the rate of recovery of product oxygen is 54%, in contrast, same 28[kilogram/(centimetre)
2] under (gauge pressure) absorption pressure,, adopt above three circulations of standard of narrating with same industrial 13X, 8 * 12 column type adsorbent of molecular sieve, total cycle time is 180 seconds, the oxygen product purity that obtains is 90%, and the BSF value is 4000 pound 13X/ ton oxygen product skies, and the rate of recovery of oxygen product has only 49%.
Persons skilled in the art will appreciate that, to the various improvement that the detail of pressure-swing absorption process of the present invention and system is made, can not depart from the present invention's of statement scope in the appended claims.They will appreciate that also pressure swing adsorption system must comprise various management, and valve and other control device realize that with suitable order adsorption bed switches to next operating procedure from an operating procedure.The present invention can select traditional pipeline and technical well-known control device at an easy rate for use.In order to realize the present invention's purpose, pressure swing adsorption system should comprise pipe-line system.At a bed from the process of higher intermediate pressure cocurrent flow decompression, gas in the product gas of the bed outlet extraction bed space, by these pipe-line systems, simultaneously with other bed in the above-mentioned gas feeding system, wherein a part of above-mentioned gas feeds a bed, carry out pressure equilibrium under above-mentioned higher intermediate pressure, some feeds the purge gas of another bed as bed.Can adopt industrial existing control system easily, make from the gas in the bed space that is in cocurrent flow decompression bed and pass through, till reaching intermediate pressure, the gas of extraction feeds the bed that is in purge step, interrupt gas then and feed bed, balance under higher pressure.Further carry out cocurrent flow depressurization steps (bed pressure is decompressed to lower intermediate pressure from above-mentioned intermediate pressure), remaining gas in the products export extraction bed space of bed, another bed in the feeding system, make each other and be issued to balance, simultaneously from the feed(raw material)inlet extraction gas of bed in lower intermediate pressure.Also disposed pipe-line system for this reason.Control system can prevent that gas from passing through a bed, and existing gas passes through when carrying out pressure equilibrium because of this bed under lower intermediate pressure.In the pressure equilibrium process, from the unstripped gas of the bed continuous extraction gas that enters the mouth, just the BD stage of E2/BD step, be decompressed to lower desorption pressure always, be issued to pressure equilibrium in low intermediate pressure.Can adopt control line valve as a kind of control device in above-mentioned back easily, above-mentioned control valve is used to prevent that the gas reflux of low intermediate pressure from going into the above-mentioned bed that is in further decompression, this bed is decompressed to lower desorption pressure from low intermediate pressure, persons skilled in the art will be understood that under suitable condition, the various improvement and the modification of adsorption process of the present invention and system, comprise and introduce other pressure equilibrium step or in partly overlapping order, also have the other adsorbent bed adsorption step that is at any given time.
Although above narration the present invention includes a constant voltage adsorption step, in contrast, three bed systems of standard comprise the adsorption step that a pressure increases progressively, no longer under constant higher absorption pressure, adsorb subsequently, but should be noted that, implement to introduce a pressure in pressure increase step as the R step in table I and the table II when of the present invention and increase progressively adsorption step, then make the supercharging of bed part by pressure equilibrium, promptly show E2 and E1 step in I and the table II, therefore, in such embodiments, bed is pressurized to higher absorption pressure, simultaneously from the products export extraction product gas of bed.In this case, in any given time, will reclaim more products gas, and can not expend the time that is used for bed regeneration, in other words can be shortlyer fixed the constant voltage adsorption step, so that there is more time to be used for carrying out the regeneration of bed, thereby make product purity and (or) rate of recovery increases, this is very favourable.Be also pointed out that the adsorption step that can advantageously adopt above-mentioned pressure to increase progressively, and combine (this system does not comprise the constant voltage adsorption step) with E2/BD step in the three-bed pressure swing adsorption system of the present invention.This operational change also is applicable to the pressure swing adsorption system that has more than three.For example implementing can to adopt operating sequence E1(to reduce pressure when of the present invention from higher absorption pressure), PP, E
2/ BD, P, the supercharging of E2(part) and will adsorb pressure and increase to higher absorption pressure.
The pressure-swing absorption process of open here and application claim and system can advantageously be used at least one component in the selective absorption raw gas mixture thereby the gas products of the needs that can separate and purify.Though, the present invention relates to separate and reclaim the component that airborne oxygen-difficulty is adsorbed, wherein nitrogen is for easily being adsorbed component, persons skilled in the art can understand other various separation processes, comprise from raw gas mixture recover hydrogen or even from unstrpped gas, separate and reclaim nitrogen as product, also be feasible, this depends on the character of the specific adsorbent that adopts in pressure swing adsorption system, and the component that is adsorbed with respect to difficulty from raw gas mixture is optionally adsorbed the ability of a component.The sorbent material that is fit to comprises zeolite molecular sieve, active carbon, silica gel, activated alumina and other materials similar.Separate from air and reclaim oxygen, generally need to use zeolite adsorbent, above-mentioned 13X adsorbent or 5A molecular sieve are standard materials, can be used for the open and application of industrial enforcement this paper for claim through improved original technology.
It will be understood that, implementing can to adopt various operating conditions when of the present invention, this depends on the specific separation process of carrying out, the purity of requirement, the sorbent material of selecting for use and other or the like.But find, particularly for from air, separating and reclaim oxygen, the higher absorption pressure of employing be about the 2.8-4.2[kilogram/(centimetre)
2] (gauge pressure), be preferably the 3.2-3.9[kilogram/(centimetre)
2] (gauge pressure) to carry out desorption under atmospheric pressure be easily, but in specific separation process, also can adopt other higher or lower desorption pressure.The present invention can make total cycle time reduce to minimum, in various embodiments, especially in four bed systems, is about 140-180 second circulation timei.Resemble table illustrate in the II embodiment in, may need longer circulation timei.These embodiments adopt five bed systems, in any given time, wherein have two beds to be in adsorption process.Compare with four bed systems that illustrate in the table I, five bed systems can obtain the higher rate of recovery.In general, when carrying out air separation with the present invention, the rate of recovery of oxygen is easy to reach in the 50%-60% scope, usually about 53-55%.
Therefore, visible the present invention can satisfy technical needed improvement, makes pressure swing adsorption can be applied to all gases lock out operation, for example separates from air and recovery oxygen.While circulation step of the present invention increases the production capacity of adsorbent, improved the capacity of bed, and compare with three pressure-swing absorption processes of industrial usefulness, the rate of recovery of product improves 5-6% approximately in cyclic process of the present invention, adopted and produced the actual purge step time weak point that the required time ratio of purge gas step provides for bed, this is favourable, because it makes total cycle time reduce to minimum, and can not reduce the purity of gas products.Therefore, the present invention has improved the feasibility that pressure swing adsorption is applied to actual industrial gasses lock out operation, and it can be used than the pressure swing adsorption of exploitation before this more profitablely.
Claims (31)
1, a kind of at the pressure swing absorption process that can be from admixture of gas optionally separates and reclaim the component that difficulty wherein is adsorbed in the adsorption system of the absorption component that easily is adsorbed wherein, wherein this adsorption system comprise at least four adsorbent bed, in each cycle period, operating sequence of each bed experience, comprise that (1) adsorb under higher adsorptive pressure, the component that is adsorbed from the products export extraction difficulty of bed is as product, (2) also stream decompression, gas in the products export extraction bed space of bed, in order to carry out pressure balance and the purpose of purge gas to be provided, with other bed in this part gas feeding system, (3) countercurrent depressurization is to lower desorption pressure, the component that easily is adsorbed from the extraction of the unstrpped gas of bed inlet, (4) under above-mentioned lower desorption pressure, purge, (5) use from the gas in the bed space of other bed and carry out pressure balance, make the supercharging of bed part and (6) be pressurized to higher adsorptive pressure, the method is characterized in that:
(a) will be from the gas in above-mentioned higher adsorptive pressure is decompressed to bed space higher intermediate pressure and that flow extraction the decompression process, another bed in the feeding system simultaneously, make it partly be pressurized to above-mentioned higher intermediate pressure, also feeding is in other second bed of low desorption pressure as purge gas.
(b) gas that continues in will the bed space of extraction from the above-mentioned bed that is in decompression process feeds above-mentioned other second bed as purge gas, makes above-mentioned bed further be decompressed to intermediate pressure from higher intermediate pressure,
(c) bed further is decompressed to lower intermediate pressure from above-mentioned intermediate pressure; Be and flow decompression; Remaining gas in the bed space of the products export extraction of bed passes into another bed the system during this period; Make it under lower intermediate pressure, carry out each other pressure balance; Meanwhile; Unstripped gas entrance extraction gas from bed; Make above-mentioned bed countercurrent depressurization; Proceed to always and finish till the above-mentioned pressure balance; The Pressure Drop of above-mentioned bed is to lower desorption pressure
Therefore,, do not make under the situation of product gas purity decline, can obtain higher adsorbent production capacity, bed capacity and product recovery rate total cycle time being reduced to minimum.
2, method according to claim 1, wherein said system comprise four adsorbent bed.
3, method according to claim 1, wherein said system comprises that 5-7 is individual adsorbent bed.
4, method according to claim 1, wherein the above-mentioned raw materials admixture of gas comprises air, and the awkward component that is adsorbed of oxygen, the component of nitrogen for easily being adsorbed.
5, method according to claim 4, wherein said system comprise 4 adsorbent bed.
6, method according to claim 5, wherein above-mentioned higher adsorptive pressure be 2.8～4.2[kilogram/(centimetre)
2] (gauge pressure).
7, method according to claim 6, wherein above-mentioned higher adsorptive pressure be 3.2～3.9[kilogram/(centimetre)
2] (gauge pressure).
8, method according to claim 7, wherein above-mentioned total cycle time are 140-180 second.
9, method according to claim 5, wherein the rate of recovery of product oxygen is 50%-60%.
10, method according to claim 8, wherein the rate of recovery of product oxygen is 53-55%.
11, method according to claim 4, wherein said system comprises 5-7 bed.
12, method according to claim 11, wherein above-mentioned higher adsorptive pressure be 2.8～4.2[kilogram/(centimetre)
2] (gauge pressure).
13, method according to claim 12, wherein above-mentioned higher adsorptive pressure be 3.2～3.9[kilogram/(centimetre)
2] (gauge pressure).
14, method according to claim 13 wherein any preset time in circulation, has two beds to be in adsorption step with partly overlapping order, and the rate of recovery of oxygen product is 50-60%.
15, method according to claim 14, wherein time heart rate of oxygen product is 53-55%.
16, method according to claim 1, the time of wherein above-mentioned generation purge gas step (b) is shorter than the time of purge step (4).
17, method according to claim 11, wherein the above-mentioned raw materials admixture of gas is an air, and the awkward component that is adsorbed of oxygen, the component of nitrogen for easily being adsorbed.
18, method according to claim 17, wherein said system comprises 4 beds, wherein above-mentioned higher adsorptive pressure be the 2.8-4.2[kilogram/(centimetre)
2] (gauge pressure), the rate of recovery of oxygen product is 50-60%, be 140-180 second total circulation timei.
19, method according to claim 17, wherein said system comprises that 5-7 is individual adsorbent bed, has two beds to overlap and is in adsorption step any preset time in circulation, the rate of recovery of oxygen product is 50-60%.
20, method according to claim 1 is wherein carried out above-mentioned pressurization, increases to higher adsorptive pressure, meanwhile, and from the products export extraction product gas of bed.
21, method according to claim 20, wherein said system comprise 4 adsorbent bed.
22, method according to claim 20, wherein said system comprises that 5-7 is individual adsorbent bed.
23, method according to claim 20, wherein above-mentioned raw gas mixture are air, and the awkward component that is adsorbed of oxygen, the component of nitrogen for easily being adsorbed.
24, method according to claim 23, wherein said system comprise 4 adsorbent bed.
25, method according to claim 23, wherein said system comprises that 5-7 is individual adsorbent bed.
26, method according to claim 23, wherein above-mentioned higher adsorptive pressure be the 2.8-4.2[kilogram/(centimetre)
2] (gauge pressure).
27, a kind of at the pressure swing absorption process that can be from admixture of gas optionally separates and reclaim the component that difficulty wherein is adsorbed in the adsorption system of the absorption component that easily is adsorbed wherein, wherein this adsorption system comprise at least three adsorbent bed, in each cycle period, operating sequence of each bed experience, comprise: (1) absorption, the component that is adsorbed from the products export extraction difficulty of bed is as product gas, (2) also stream decompression, gas in the products export extraction layer space of bed, in order to carry out pressure balance and the purpose of purge gas to be provided, with other bed in this part gas feeding system, (3) countercurrent depressurization is to lower desorption pressure, easily be adsorbed component from the unstrpped gas inlet extraction of bed, (4) purge under above-mentioned lower desorption pressure, (5) are used from the gas in the bed space of other bed and are carried out pressure balance, make the supercharging of bed part, (6) further be pressurized to higher adsorptive pressure, the method is characterized in that:
(a) with the gas of bed in above-mentioned higher adsorptive pressure is decompressed to bed space higher intermediate pressure and that flow extraction the decompression process, another bed in the feeding system, make above-mentioned another bed partly be pressurized to above-mentioned higher middle pressure
(b) with the remaining gas of bed in above-mentioned higher intermediate pressure further is decompressed to bed space intermediate pressure and that flow extraction the decompression process, different beds in the part feeding system, the remaining gas in the bed space of above-mentioned extraction is as the purge gas of above-mentioned another one bed.
(c) that bed further is decompressed to lower intermediate pressure again from above-mentioned intermediate pressure and flow the decompression process, be in the another one bed of lower pressure in the residual gas feeding system in the bed space of extraction at first, make each other and under above-mentioned lower intermediate pressure, carry out balance, simultaneously from the unstripped gas inlet extraction gas of the bed that is in decompression process, make the bed countercurrent depressurization
(d) discontinuously the gas in the above-mentioned bed space is fed the bed that is in lower pressure at first, make above-mentioned bed decompression, the above-mentioned bed that is in lower pressure at first reaches above-mentioned lower intermediate pressure,
(e) further make the above-mentioned bed countercurrent depressurization that is in depressurization steps continuously, after finishing above-mentioned steps (c), the pressure of above-mentioned bed is reduced to lower desorption pressure,
(f) component that is adsorbed from the products export extraction difficulty of bed is as product gas, and the unstripped gas inlet from this bed feeds raw gas mixture simultaneously, makes the bed of part supercharging be pressurized to above-mentioned higher adsorptive pressure, and
(g) when cycling is carried out continuously, add other a certain amount of unstrpped gas, repeat above-mentioned (a)-(f) step, beginning to carry out before cocurrent flow is decompressed to higher intermediate pressure, under higher adsorptive pressure, do not feed unstrpped gas and adsorb, and the component that therefrom extraction difficulty is adsorbed under constant higher adsorptive pressure.
28, method according to claim 27, wherein said system comprise four adsorbent bed.
29, method according to claim 27, wherein said system comprises that 5-7 is individual adsorbent bed.
30, method according to claim 27, wherein the above-mentioned raw materials admixture of gas is an air, wherein oxygen is embarrassed the component that is adsorbed, the component of nitrogen for easily being adsorbed.
31, method according to claim 30, wherein above-mentioned higher adsorptive pressure be the 2.8-4.2[kilogram/(centimetre)
2] (gauge pressure).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 86102699 CN1010378B (en) | 1986-04-18 | 1986-04-18 | Improved differential pressure adsorption process and equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 86102699 CN1010378B (en) | 1986-04-18 | 1986-04-18 | Improved differential pressure adsorption process and equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN86102699A CN86102699A (en) | 1987-10-28 |
| CN1010378B true CN1010378B (en) | 1990-11-14 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 86102699 Expired CN1010378B (en) | 1986-04-18 | 1986-04-18 | Improved differential pressure adsorption process and equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1010378B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101987804B1 (en) * | 2017-11-17 | 2019-06-12 | 한국에너지기술연구원 | Pressure swing adsorption method and pressure swing adsorption apparatus |
| CN108333117B (en) * | 2017-12-26 | 2021-02-09 | 聚光科技(杭州)股份有限公司 | In-situ type pipeline gas detection device and working method thereof |
| US10744450B2 (en) * | 2018-08-14 | 2020-08-18 | Air Products And Chemicals, Inc. | Multi-bed rapid cycle kinetic PSA |
-
1986
- 1986-04-18 CN CN 86102699 patent/CN1010378B/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| CN86102699A (en) | 1987-10-28 |
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