CN105169889A - Pressure swing adsorption process for cascade purging - Google Patents
Pressure swing adsorption process for cascade purging Download PDFInfo
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- CN105169889A CN105169889A CN201510701592.4A CN201510701592A CN105169889A CN 105169889 A CN105169889 A CN 105169889A CN 201510701592 A CN201510701592 A CN 201510701592A CN 105169889 A CN105169889 A CN 105169889A
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Abstract
The invention discloses a pressure swing adsorption process for cascade purging. The process comprises the following steps: adsorption, uniform pressure drop, normal release, inverse release, purging 1, purging 2, uniform pressure rise, and purging ending, wherein purging gas is provided by the normal release step and/or the uniform pressure rise step; after the purging gas enters a first adsorption tower in the purging step for purging, purging waste gas of the first adsorption tower enters a second adsorption tower in the purging step to purge the second adsorption tower, and the purging waste gas of the second adsorption tower is discharged from a pressing swing adsorption device or is used for purging a third adsorption tower or more subsequent adsorption towers, so that two or more than two adsorption towers can be purged in a cascaded way by using the purging gas. By using the pressure swing adsorption process for cascade purging, provided by the invention, equipment such as a normal gas release buffer tank does not need to be additionally arranged, so that the use efficiency of the purging gas can be improved, the use amount of the purging gas can be reduced, the product yield can be improved, normal release time and total circulating time can be shortened, and adsorbent dosage and equipment investment can be remarkably reduced.
Description
Technical field
The invention belongs to chemical field, relate to the PSA Gas Separation Technology in chemical field, especially use the method for purging method regeneration, be specially the pressure swing adsorption technique that a kind of tandem is rinsed.
Background technology
PSA Gas Separation Technology take pressure as thermodynamic parameter, and gas component absorption under stress, by absorbed component desorb under decompression, discharge this gas component, adsorbent is regenerated.Common decompression renovation process has two kinds, and the first vacuumizes and reduces gas phase stagnation pressure; Its two be rinse reduce by the dividing potential drop of absorbed component.Owing to rinsing regeneration without the need to using vavuum pump, saving investment, reducing energy consumption, therefore in recent years, again becoming the focus of research.
Along with the material gas quantity of pressure-swing absorption apparatus process is increasing, the equipment such as adsorption tower, caliber, valve of pressure-swing absorption apparatus also becomes increasing.But the crushing strength of sorbent suspension particle limits, and considers the manufacture of adsorption tower, the difficulty of transport, and adsorption tower size can not infinitely become large.Under the prerequisite ensureing product quality, user often requires that less investment and floor space, obtain higher yield with less equipment.For meeting above requirement, there are following two kinds of methods: one is the utilization ratio improving purge gas, to reduce flushing tolerance, reach the object improving product yield; Two is shorten total cycle time, improves the utilization ratio of adsorbent, to reach minimizing adsorbent amount, reduces the object of investment and minimizing floor space.
Existing pressure swing adsorption technique, all adopt douching technique in parallel, namely purge gas is split into a or several parts, be respectively used to rinse different adsorption towers, the flushing waste gas of each adsorption tower, all discharge from pressure swing adsorption cycles, can not reuse, this makes purge gas fail to be fully used.Particularly after rinsing the phase time to rinse the impurity content of waste gas lower, and this partial flushing waste gas also can be discharged from pressure swing adsorption cycles, makes this partial flushing waste gas to fail to be fully used, and can affect the yield of product.
ZL01112382.6 discloses a kind of large-scale variable-pressure adsorptive process, the method by multiple adsorption tower simultaneously for multiple adsorption tower provides purified gas, break the convention that the purifying step time should be equal to or less than the adsorption step time, adsorption time and total cycle time are all significantly reduced, adsorbent amount and equipment investment can be reduced, also under the constant prerequisite of product purity yield, the unstripped gas treating capacity of device can be increased.
ZL200510020305.X discloses the pressure swing adsorption technique of band two downflow releasing tanks, the adsorption tower of pressure-swing absorption apparatus is divided into two series by this technique, each array configuration downflow releasing tank is for storing the suitable venting for adsorption tower regeneration, the suitable of each series is put and flush loop configures sequencing valve and control valve, and its sequential is as shown in table 1.
The 10-3-4 process timing sequence of table 1 with two downflow releasing tanks
This technique can under the prerequisite ensureing the same recovery time, greatly shorten adsorption time and along putting the time, reduce the volume of adsorption tower and the total amount of adsorbent, thus greatly reduce investment outlay, also can realize two serial adsorption towers to rinse respectively or turn interleaving flushing, there is better regeneration effect, thus improve the product recovery rate of device.
ZL200810044290.4 discloses multiple placing in turn interleaving flushing pressure variable adsorption technique, this technique is set up along discharge port valve, is rinsed inlet valve and at least four control valves be interspersed on adsorption tower top exit pipeline, achieve more than three times or three times along putting and flushing process, add the recovery time, reduce absorption and divide cycle time, reduce purge gas consumption, can effectively improve gas product yield, and reduce the investment of device and reduce floor space.And each adsorption tower is completely the same along putting flushing process, avoids the regeneration effect reducing whole device because of the performance difference of control valve.
Above technological process control all belongs in parallel and rinses, and the flushing waste gas of each tower is all discharged from absorption regeneration circulation, rinses waste gas and fails to be fully used.
Summary of the invention
For above-mentioned the deficiencies in the prior art, the invention provides the pressure swing adsorption technique that a kind of tandem is rinsed, purge gas tandem can be recycled, improve the utilization ratio of purge gas, reduce and rinse exhausted air quantity, improve product yield, also can increase washing time simultaneously, shorten total cycle time, significantly reduce adsorbent amount and equipment investment.
Technical scheme of the present invention is:
The pressure swing adsorption technique that a kind of tandem is rinsed, this technique at least comprises the following steps, absorption, equal pressure drop, along putting, inverse put, rinse 1, rinse 2, equal voltage rise, fill step eventually, along strideing, rapid and/or equal voltage drop step provides purge gas, this purge gas enters after first adsorption tower being in rinsing step rinse, the flushing waste gas of first adsorption tower enters the adsorption tower that second is in rinsing step, second adsorption tower is rinsed, the flushing waste gas of second adsorption tower to be discharged or to the 3rd or rinse adsorption towers more below from pressure-swing absorption apparatus, realize purge gas to rinse two or more adsorption tower tandem.
Adsorption tower after described inverse put step enters equal voltage rise step after n time is rinsed, first adsorption tower that tandem is rinsed is the adsorption tower being about to enter equal voltage rise, this rinsing step is called n-th flushing, namely n is rinsed, the flushing waste gas rinsing n goes to rinse n-1, and by that analogy, last adsorption tower that tandem is rinsed is just through the adsorption tower of inverse put step, be called that first time rinses, namely rinse 1.
Described pressure-swing absorption apparatus is configured with the sequencing valve and pipeline that all adsorption towers are together in series by a row, and after all adsorption towers arrange in order, got up by sequencing valve and placed in series in the bottom of every platform adsorption tower and the top of next adsorption tower.
At least two comb lines are had above described adsorption tower, the pipeline of one row for providing purge gas, another row, for rinsing admission line, is connected by sequencing valve between each adsorption tower with this two combs line, provides between the pipeline of purge gas with flushing admission line and is connected by control valve.
The tandem number that described tandem is rinsed is 2-5 level, and namely n is 2-5, and tandem number is preferably 2-3 level, and namely n is preferably 2-3.
Flushing pressure in described rinsing step is 0.01-0.1MPa (G).
Use the method for rinsing to regenerate, be generally used for the situation obtaining product from fluid phase.Rinse the effect of regeneration, depend primarily on amount and the washing time of purge gas, rinse regeneration effect better, the dynamic adsorbance of adsorbent is larger, and quantity of sorbent needed for the unstripped gas processing identical amount just less.Rinse the product yield of renovation process, lose with the active principle lost in flushing waste gas, rinse the active principle lost in waste gas fewer, product yield is higher.
The present invention, under the condition that the flushing tolerance that rapid and/or equal voltage drop step provides along strideing is identical, often goes here and there one-level, and total flushing tolerance that can double, total washing time also significantly increases, and developing result can obviously be promoted.Therefore in practical operation, the flushing tolerance provided can be provided, the developing result identical with other purging method can be obtained along rapid and/or equal voltage drop step of strideing.After rinsing tolerance minimizing, rinse exhausted air quantity and also can reduce thereupon, and owing to taking tandem to rinse, the impurity concentration of rinsing in waste gas raises, and product design reduces, therefore the product lost from flushing waste gas reduces, the product yield obtained from fluid phase raises.When not increasing downflow releasing tank, the rinsing step time of the present invention strides the rapid time much larger than suitable, and it is at least suitable with the adsorption step time, therefore in practical operation, a point cycle time can be reduced, then can reduce adsorption time and total cycle time, thus reach the object reducing adsorbent amount and reduce equipment investment.
Good effect of the present invention is embodied in:
(1), the pressure swing adsorption technique that rinses of the tandem that uses of the present invention, the service efficiency of purge gas can be improved, reduce purge gas consumption, improve product yield;
(2) pressure swing adsorption technique that the tandem that, the present invention uses is rinsed, the rinsing step time strides the rapid time much larger than suitable, and at least suitable with the adsorption step time, adsorption time and total cycle time shorter, can significantly reduce adsorbent amount and equipment investment;
(3), the present invention use tandem rinse pressure swing adsorption technique, without the need to use along venting surge tank.
Accompanying drawing explanation
Fig. 1 is the process unit schematic diagram adopted in embodiment 1 and embodiment 2 in the present invention;
Fig. 2 is the process unit schematic diagram adopted in embodiment 3 in the present invention;
Fig. 3 is the process unit schematic diagram adopted in embodiment 4 in the present invention.
Detailed description of the invention
Below by way of the embodiment of detailed description of the invention, the present invention is further detailed explanation, but this should be interpreted as that the scope of the above-mentioned theme of the present invention is only limitted to following embodiment.Without departing from the idea case in the present invention described above, the various replacement made according to ordinary skill knowledge and customary means or change, include within the scope of the invention.
Embodiment 1:
The present embodiment adopts 10 tower two-stage series connection developing techniques, and the raw gas pressure of process is 2.5MPa, and in unstripped gas, the content of hydrogen is 70%, and product hydrogen content is 99.9%.As shown in Figure 1, process timing sequence is as shown in table 2 for the device of this embodiment:
Table 210 tower two-stage series connection developing technique time-scale
For adsorption tower A, after unstripped gas enters adsorption tower A, the product that hydrogen content is 99.9% is obtained from tower top, after adsorption step (A), adsorption tower A carries out one equal (1D), two equal (2D) and three equal (3D) respectively with tower D, tower E, tower F, after all pressing for three times, enter along stride rapid (PP).
The gas forward bleeding off pressure out from adsorption tower A is as purge gas, and carry out second time by control valve PV01 to adsorption tower H and rinse, before this step, adsorption tower H lives through once flushing.From adsorption tower H flushing waste gas out, impurities content is relatively less, enters adsorption tower I through sequencing valve KV109, continues to rinse adsorption tower I, from adsorption tower I flushing waste gas out, is disposed to stripping gas surge tank.
Along strideing suddenly, adsorption tower A and tower H carries out the 4th time and all presses (4D), residual gas in tower, then by inverse put step (D), discharges from adsorbent equipment, and the Pressure Drop of adsorption tower is to about 0.02MPa.
After inverse put step, adsorption tower A carries out first time and rinses (P1).From adsorption tower C along venting, through control valve PV01, first carry out second time to tower J and rinse, from tower J flushing waste gas out, carry out first time flushing through KV101 to tower A, now, the most of impurity in adsorption tower A, is rinsed out.
After first time flushing, adsorption tower A carries out second time and rinses (P2).From the suitable venting of adsorption tower D, through control valve PV01, carry out second time to adsorption tower A and rinse, adsorption tower A obtains holomorphosis.From adsorption tower A flushing waste gas out, impurities content is relatively less, continues to recycle, enter adsorption tower B through KV102 to this partial flushing waste gas, carries out first time rinse adsorption tower B.
Regenerate clean adsorption tower A, four equal (4R), three equal (3R), two equal (2R) and one equal (1R) is carried out respectively with tower D, tower F, tower G, tower H, again by filling (FR) eventually, boost to adsorptive pressure.Complete an absorption regeneration circulation.
By this 10 tower two-stage series connection developing technique, the comparable typical developing technique in parallel of the suitable discharge quantity that every tower need provide reduces about 20%, the comparable typical developing technique increase about 60% in parallel of total flushing tolerance that every tower obtains, total washing time increase about 11%, total cycle time reduces about 17%, and hydrogen yield can reach 91%.In PSA method, the expense of total cycle time and equipment has direct relation, and total cycle time is shorter, and expense is lower.Total flushing tolerance is more, and washing time is longer, and adsorbent reactivation effect is better.Shorter along putting the time, be more conducive to shortening total cycle time.
Embodiment 2:
The present embodiment adopts 10 tower thtee-stage shiplock developing techniques, and the raw gas pressure of process is 2.5MPa, and in unstripped gas, the content of hydrogen is 70%, and product hydrogen content is 99.9%.As shown in Figure 1, process timing sequence is as shown in table 3 for the device of this embodiment:
Table 310 tower thtee-stage shiplock developing technique time-scale
For adsorption tower A, after unstripped gas enters adsorption tower A, obtain from tower top the product that hydrogen content is 99.9%, after adsorption step, adsorption tower A carries out one all and two all respectively with tower D, tower E, all after pressure, enters along strideing rapid twice.
The gas forward bleeding off pressure out from adsorption tower A is as purge gas, and carry out third time by control valve PV01 to adsorption tower G and rinse, before this step, adsorption tower G has lived through twice flushing.From adsorption tower G flushing waste gas out, impurities content is relatively less, enters adsorption tower H through sequencing valve KV108, continues to rinse adsorption tower H, and before this step, adsorption tower H lives through once flushing.From adsorption tower H flushing waste gas out, impurities content than many from adsorption tower G flushing waste gas out, but still has the value recycled, adsorption tower I is entered through sequencing valve KV109, continue to rinse adsorption tower I, from adsorption tower I flushing waste gas out, be disposed to stripping gas surge tank.
Along strideing suddenly, adsorption tower A and tower G carries out third time and all presses, residual gas in tower, then by inverse put step, discharges from adsorbent equipment, and the Pressure Drop of adsorption tower is to about 0.02MPa.
After inverse put step, adsorption tower A carries out first time and rinses.From the suitable venting of adsorption tower C, through control valve PV01, first carry out third time to tower I to rinse, from tower I flushing waste gas out, through KV110, second time is carried out to tower J and rinse, from tower J flushing waste gas out, carry out first time through KV101 to tower A to rinse, now, the partial impurities in adsorption tower A, is rinsed out.
After first time flushing, adsorption tower A carries out second time and rinses.From adsorption tower D along venting, through control valve PV01, carry out third time rinse adsorption tower J, from tower J flushing waste gas out, carry out second time flushing through KV101 to tower A, adsorption tower A continues to be reproduced.From adsorption tower A flushing waste gas out, enter adsorption tower B through KV102, first time is carried out to adsorption tower B and rinses.
After second time is rinsed, adsorption tower A carries out third time and rinses.From the suitable venting of adsorption tower E, through control valve PV01, carry out third time to adsorption tower A and rinse, adsorption tower A obtains holomorphosis.From tower A flushing waste gas out, enter adsorption tower B through KV102, second time is carried out to tower B and rinses.From adsorption tower B flushing waste gas out, enter adsorption tower C through KV103, first time is carried out to tower C and rinses.
Regenerate clean adsorption tower A, carry out with tower E, tower G, tower H respectively three all, two all and one all, then by filling eventually, boost to adsorptive pressure.Complete an absorption regeneration circulation.
By this 10 tower thtee-stage shiplock developing technique, the comparable typical developing technique in parallel of the suitable discharge quantity that every tower need provide reduces about 20%, the comparable typical developing technique increase about 140% in parallel of total flushing tolerance that every tower obtains, total washing time increase about 33%, total cycle time reduces about 33%, and hydrogen yield can reach 91%.
Compared with embodiment 1, the total cycle time of the present embodiment is shorter, and adsorbent amount is less, and cost of equipment is lower.
Embodiment 3:
The present embodiment adopts 12 tower thtee-stage shiplock developing techniques, and the raw gas pressure of process is 2.5MPa, and in unstripped gas, the content of hydrogen is 70%, and product hydrogen content is 99.9%.As shown in Figure 2, process timing sequence is as shown in table 4 for the device of this embodiment:
Table 412 tower thtee-stage shiplock developing technique time-scale
For adsorption tower A, after unstripped gas enters adsorption tower A, obtaining from tower top the product that hydrogen content is 99.9%, after adsorption step, adsorption tower A carries out with tower E, tower F, tower G one all respectively, two all and three all, all after pressure, entering along strideing rapid three times.
The gas forward bleeding off pressure out from adsorption tower A is as purge gas, and carry out third time by control valve PV01 to adsorption tower I and rinse, before this step, adsorption tower I has lived through twice flushing.From adsorption tower I flushing waste gas out, impurities content is relatively less, enters adsorption tower J through sequencing valve KV110, continues to rinse adsorption tower J, and before this step, adsorption tower J lives through once flushing.From adsorption tower J flushing waste gas out, impurities content than many from adsorption tower I flushing waste gas out, but still has the value recycled, adsorption tower K is entered through sequencing valve KV111, continue to rinse adsorption tower K, from adsorption tower K flushing waste gas out, be disposed to stripping gas surge tank.
Along strideing suddenly, adsorption tower A and tower I carries out the 4th time and all presses, residual gas in tower, then by inverse put step, discharges from adsorbent equipment, and the Pressure Drop of adsorption tower is to about 0.02MPa.
After inverse put step, adsorption tower A carries out first time and rinses.From the suitable venting of adsorption tower C, through control valve PV01, first carry out third time to tower K to rinse, from tower K flushing waste gas out, through KV112, second time is carried out to tower L and rinse, from tower L flushing waste gas out, carry out first time through KV101 to tower A to rinse, now, the partial impurities in adsorption tower A, is rinsed out.
After first time flushing, adsorption tower A carries out second time and rinses.From adsorption tower D along venting, through control valve PV01, carry out third time rinse adsorption tower L, from tower L flushing waste gas out, carry out second time flushing through KV101 to tower A, adsorption tower A continues to be reproduced.From adsorption tower A flushing waste gas out, enter adsorption tower B through KV102, first time is carried out to adsorption tower B and rinses.
After second time is rinsed, adsorption tower A carries out third time and rinses.From the suitable venting of adsorption tower E, through control valve PV01, carry out third time to adsorption tower A and rinse, adsorption tower A obtains holomorphosis.From tower A flushing waste gas out, enter adsorption tower B through KV102, second time is carried out to tower B and rinses.From adsorption tower B flushing waste gas out, enter adsorption tower C through KV103, first time is carried out to tower C and rinses.
Regenerate clean adsorption tower A, carry out with tower E, tower G, tower H, tower I respectively four all, three all, two all and one all, then by filling eventually, boost to adsorptive pressure.Complete an absorption regeneration circulation.
By this 12 tower thtee-stage shiplock developing technique, the comparable typical developing technique in parallel of the suitable discharge quantity that every tower need provide reduces about 20%, the comparable typical developing technique increase about 140% in parallel of total flushing tolerance that every tower obtains, total washing time increase about 33%, total cycle time reduces about 33%, and hydrogen yield can reach 93%.
Embodiment 4:
The present embodiment adopts 8 tower two-stage series connection developing techniques, and the raw gas pressure of process is 2.5MPa, and in unstripped gas, the content of hydrogen is 70%, and product hydrogen content is 99.9%.As shown in Figure 3, process timing sequence is as shown in table 5 for the device of this embodiment:
Table 58 tower two-stage series connection developing technique time-scale
For adsorption tower A, after unstripped gas enters adsorption tower A, obtain from tower top the product that hydrogen content is 99.9%, after adsorption step, adsorption tower A carries out one all and two all respectively with tower C, tower D, all after pressure, enters along strideing rapid twice.
The gas forward bleeding off pressure out from adsorption tower A is as purge gas, and carry out second time by control valve PV01 to adsorption tower F and rinse, before this step, adsorption tower F lives through once flushing.From adsorption tower F flushing waste gas out, impurities content is relatively less, enters adsorption tower G through sequencing valve KV107, continues to rinse adsorption tower G, from adsorption tower G flushing waste gas out, is disposed to stripping gas surge tank.
Along strideing suddenly, adsorption tower A and tower F carries out third time and all presses, residual gas in tower, then by inverse put step, discharges from adsorbent equipment, and the Pressure Drop of adsorption tower is to about 0.02MPa.
After inverse put step, adsorption tower A carries out first time and rinses.From adsorption tower C along venting, through control valve PV01, first carry out second time to tower H and rinse, from tower H flushing waste gas out, carry out first time flushing through KV101 to tower A, now, the most of impurity in adsorption tower A, is rinsed out.
After first time flushing, adsorption tower A carries out second time and rinses.From the suitable venting of adsorption tower D, through control valve PV01, carry out second time to adsorption tower A and rinse, adsorption tower A obtains holomorphosis.From adsorption tower A flushing waste gas out, impurities content is relatively less, continues to recycle, enter adsorption tower B through KV102 to this partial flushing waste gas, carries out first time rinse adsorption tower B.
Regenerate clean adsorption tower A, carry out with tower D, tower F, tower G respectively three all, two all and one all, then by filling eventually, boost to adsorptive pressure.Complete an absorption regeneration circulation.
By this 8 tower two-stage series connection developing technique, the comparable typical developing technique in parallel of the suitable discharge quantity that every tower need provide reduces about 20%, the comparable typical developing technique increase about 60% in parallel of total flushing tolerance that every tower obtains, total washing time increase about 11%, total cycle time reduces about 17%, and hydrogen yield can reach 88%.
Claims (7)
1. the pressure swing adsorption technique of a tandem flushing, this technique at least comprises the following steps, absorption, equal pressure drop, along putting, inverse put, rinse 1, rinse 2, equal voltage rise, fill step eventually, along strideing, rapid and/or equal voltage drop step provides purge gas, it is characterized in that: this purge gas enters after first adsorption tower being in rinsing step rinse, the flushing waste gas of first adsorption tower enters the adsorption tower that second is in rinsing step, second adsorption tower is rinsed, the flushing waste gas of second adsorption tower to be discharged or to the 3rd or rinse more adsorption tower below from pressure-swing absorption apparatus, realize purge gas to rinse two or more adsorption tower tandem.
2. the pressure swing adsorption technique of tandem flushing according to claim 1, it is characterized in that: the adsorption tower after described inverse put step enters equal voltage rise step after n time is rinsed, first adsorption tower that tandem is rinsed is the adsorption tower being about to enter equal voltage rise, this rinsing step is called n-th flushing, namely rinses n, and the flushing waste gas rinsing n goes to rinse n-1, by that analogy, last adsorption tower that tandem is rinsed is just through the adsorption tower of inverse put step, is called that first time rinses, namely rinses 1.
3. the pressure swing adsorption technique of tandem flushing according to claim 1, it is characterized in that: described pressure-swing absorption apparatus is configured with the sequencing valve and pipeline that all adsorption towers are together in series by a row, after all adsorption towers arrange in order, got up by sequencing valve and placed in series in the bottom of every platform adsorption tower and the top of next adsorption tower.
4. the pressure swing adsorption technique of tandem flushing according to claim 1, it is characterized in that: above adsorption tower, have at least two comb lines, the pipeline of one row for providing purge gas, another row is for rinsing admission line, be connected by sequencing valve between each adsorption tower with this two combs line, provide between the pipeline of purge gas with flushing admission line and be connected by control valve.
5. the pressure swing adsorption technique that tandem is rinsed according to claim 1 or claim 2, is characterized in that: the tandem number that described tandem is rinsed is 2-5 level, and namely n is 2-5.
6. the pressure swing adsorption technique that tandem is rinsed according to claim 1 or claim 2, is characterized in that: the tandem number that described tandem is rinsed is 2-3 level, and namely n is 2-3.
7. the pressure swing adsorption technique of tandem flushing according to claim 1, is characterized in that: the flushing pressure in described rinsing step is 0.01-0.1MPa(G).
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108310909A (en) * | 2017-01-17 | 2018-07-24 | 四川天采科技有限责任公司 | A method of p-phthalic acid's tail gas pressure-variable adsorption containing CO extracts H2 |
| CN113041782A (en) * | 2021-03-15 | 2021-06-29 | 西南化工研究设计院有限公司 | Gas pressure swing adsorption separation and purification system and separation and purification method thereof |
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| CN1175474A (en) * | 1997-04-14 | 1998-03-11 | 成都华西化工研究所 | Multi-tower pressure swing adsorption method and apparatus for separation of gas |
| CN101396632A (en) * | 2008-10-27 | 2009-04-01 | 四川亚连科技有限责任公司 | Multi-stage absorption, regeneration and purification method of polysilicon tail gas |
| CN101732945A (en) * | 2009-12-25 | 2010-06-16 | 成都赛普瑞兴科技有限公司 | Method for recovering hydrogen from tail gas containing chlorsilane |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1175474A (en) * | 1997-04-14 | 1998-03-11 | 成都华西化工研究所 | Multi-tower pressure swing adsorption method and apparatus for separation of gas |
| CN101396632A (en) * | 2008-10-27 | 2009-04-01 | 四川亚连科技有限责任公司 | Multi-stage absorption, regeneration and purification method of polysilicon tail gas |
| CN101732945A (en) * | 2009-12-25 | 2010-06-16 | 成都赛普瑞兴科技有限公司 | Method for recovering hydrogen from tail gas containing chlorsilane |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108310909A (en) * | 2017-01-17 | 2018-07-24 | 四川天采科技有限责任公司 | A method of p-phthalic acid's tail gas pressure-variable adsorption containing CO extracts H2 |
| CN108310909B (en) * | 2017-01-17 | 2020-06-19 | 四川天采科技有限责任公司 | Method for extracting H2 from CO-containing purified terephthalic acid tail gas through pressure swing adsorption |
| CN113041782A (en) * | 2021-03-15 | 2021-06-29 | 西南化工研究设计院有限公司 | Gas pressure swing adsorption separation and purification system and separation and purification method thereof |
| CN113041782B (en) * | 2021-03-15 | 2021-12-17 | 西南化工研究设计院有限公司 | Gas pressure swing adsorption separation and purification system and separation and purification method thereof |
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Application publication date: 20151223 |
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