CN1089621C - Multi-tower pressure-changeable gas-adsorption separation method - Google Patents
Multi-tower pressure-changeable gas-adsorption separation method Download PDFInfo
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- CN1089621C CN1089621C CN96117584A CN96117584A CN1089621C CN 1089621 C CN1089621 C CN 1089621C CN 96117584 A CN96117584 A CN 96117584A CN 96117584 A CN96117584 A CN 96117584A CN 1089621 C CN1089621 C CN 1089621C
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- adsorption separation
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Abstract
The present invention relates to a multi-tower pressure-changeable gas-adsorption separation method. Each tower comprises the steps of adsorption (A), pressure equalizing and dropping (ED), forward outgassing flushing or vacuating (VC), pressure equalizing and rising (ER) and final pressure rising (FR). The forward outgassing flashing/vacuating steps of the towers are continuous or partially overlapped. According to the number of the towers in the absorption state at the same time, the absorption towers are divided into the number of groups, and the vacuating steps of the towers in each group are discontinuous. Each group of absorption towers are connected to a desorption pipe line and a vacuum pump. The desorption pipelines are connected via sequence valves. The desorption pipelines are provided with the sequence valves without need of vacuum buffer tanks, so the present invention can eliminate or shorten isolation steps in the process, shorten a process cycle, raise gas yield and productive efficiency, reduce energy consumption and greatly reduce equipment investment.
Description
The present invention is relevant with pressure-changeable gas-adsorption separation method, and is especially relevant with multitower PSA pressure-changeable gas-adsorption separation method.
Traditional pressure-changeable gas-adsorption separation method needs two or more adsorption towers at least.Each adsorption tower once generally will experience absorption (A) in the circulation, and drop pressure (ED) forward or reverse pressures (D) of putting, is suitablely put air blast method or vacuumized (VC), boost pressure (ER), isolation (I), (FR) step of finally boosting.Usually the tower number that is in adsorbed state in the multitower system all the time is more than 2 or 2.Some time also has two adsorption towers and is in the regeneration stage of washing or vacuumizing along venting simultaneously.When adopting, can avoid the phase mutual interference by increasing the desorb pipeline along the venting back flush.But when adopting vacuum desorption regeneration, because vavuum pump can not pause, and the step that vacuumizes on the PSA pressure swing adsorption technique step procedure is not continuous, traditional solution is a parallel connection vacuum surge tank on vacuum lines, when vavuum pump can not directly be taken out tower, just take out surge tank, cause investment and energy consumption to increase thus.Traditional PSA pressure-changeable gas-adsorption separation method since forward or reverse putting press step and vacuumize or all on same desorb pipeline, carry out along the venting rinsing step, isolation time is long.
The purpose of this invention is to provide a kind of vacuum buffer tank that do not need, cut down the consumption of energy, isolation (or waiting for maintenance) step in elimination or the shortening PSA processing step, the gas recovery ratio height, quality is good, production efficiency height, the multi-tower pressure-changeable gas-adsorption separation method that installation cost is low.
The cycle period of PSA adsorption tower of the present invention all includes absorption (A), drop pressure (ED), and suitable venting is washed or is vacuumized (VC), boost pressure (ER), (FR) step of finally boosting.Each tower along venting flushing or vacuumize step continuously or overlap, each tower is connected with the desorb pipeline by sequencing valve, the desorb pipeline is connected with vavuum pump again.
The present invention can be divided into the group of this number with adsorption tower by the number that synchronization is in the tower of adsorbed state, in every group tower to vacuumize step discontinuous.Every group of adsorption tower connects one tunnel desorb pipeline and vavuum pump.Connect with sequencing valve between the desorb pipeline, on the desorb pipeline sequencing valve is arranged.
The number that synchronization of the present invention is in the tower of adsorbed state can be two or more.
Each tower of the present invention forward or reverse putting press step (D) and vacuumize or carry out simultaneously by different desorb pipelines along the rinsing step (VC) of exitting.
The present invention is discontinuous along venting flushing or vacuumize step and change into continuously or overlap with each tower, the number that is in the tower of adsorbed state by synchronization is divided into adsorption tower the group of this number, the regeneration step of tower is discontinuous in every group, every winding one tunnel desorb pipeline and vavuum pump, connect with sequencing valve between the desorb pipeline, when wherein the vavuum pump of a pipeline requires to vacuumize continuously the tower of this group because of the PSA processing step, open the sequencing valve between pipeline, then this group vavuum pump assists another group tower is vacuumized, and vice versa.Can save the bigger vacuum buffer tank of volume.Because whole process all is directly to take out tower by vavuum pump, has reduced energy consumption.Forward or reverse putting press step and vacuumize regeneration step and can carry out simultaneously by different desorb pipelines, processing step is compact more, shorten or eliminated isolation time, thereby accelerated cycle period, improved the adsorbent utilization rate, reduce installation cost, improved the yield and the productivity ratio of product gas.
Fig. 1 is the traditional handicraft installation drawing.
Fig. 2 is a process device figure of the present invention.
Fig. 3 is an another kind of installation drawing of the present invention.
Fig. 4 is the present invention's nine tower flow charts.
Fig. 5 is traditional handicraft four-column process flow figure.
Fig. 6 is the present invention's six tower flow charts.
Fig. 7 is the another kind of six tower flow charts of the present invention.
Following is embodiments of the invention:
The traditional handicraft device is commonly referred to the 4-1-2 flow process, promptly 4 represents four adsorption towers, 1 the representative all the time one be in adsorbed state, 2 represent twice all the pressure.Technology of the present invention can be at 4-2-1,5-2-1,5-2-2,6-2-2,6-2-3,7-2-1,7-2-2,7-2-3,8-2-3,8-3-2,8-3-1,9-3-2,9-3-3,10-3-3,10-4-2, implement on any multitower pressure-swing absorption apparatus such as 10-4-3, any those skilled in the art all can promote by method of the present invention, but this popularization does not exceed method of the present invention.
Embodiment 1:
Traditional pressure swing adsorption method removes CO from conversion gas
2, get product gas H
2And N
2, its four-column process flow as shown in Figure 1.
From four tower working procedure Fig. 5 as can be seen, it is discontinuous vacuumizing step VC, therefore, must establish vacuum buffer tank.This tank volume 15m
3Vaccum pump motor is 60KW altogether, design operation pressure 0.8MPa, design disposal ability 3000Nm
3/ h.The actual running results is: handle tolerance 2300Nm
3/ h, H
2Yield 93%, CO in the product hydrogen and nitrogen gas
2≤ 0.4%.
Utilize the present invention to transform above-mentioned traditional handicraft, increase by two adsorption towers of same volume on the basis of Yuan Sita, the cancellation vacuum tank increases by one tunnel desorb route and one group of vavuum pump flow chart such as Fig. 2.Motor is 150KW.Six tower working procedure tables of the present invention are pressed tower A, C, E and tower B, D, F grouping as shown in Figure 6, and the evacuation step VC between each group is discontinuous, and two groups evacuation step is continuous, and partly overlapping.
As can be seen from Figure 6, the present invention has 2 at the tower that synchronization is in adsorbed state.When vacuumizing step when overlapping, shut off valve 5, each vavuum pump pairing adsorption tower of finding time, when vacuumizing step VC when not overlapping, open valve 5,2, one groups of vavuum pumps of shut off valve 1 or valve just assist another group vavuum pump to take out adsorption tower, because every group of vavuum pump can both directly be taken out adsorption tower all the time, just vacuum buffer tank needn't have been used.Valve 3,4 is the contrary sequencing valve of putting.
This example is handled tolerance and is reached 8000Nm
3/ h.H
2Yield＞98.5%, CO in the product hydrogen and nitrogen gas
2≤ 0.2%.
Embodiment 2:
The same example of hardware unit adopts two desorb pipelines and two groups of vavuum pumps, and 6 adsorption towers have two to be in adsorbed state all the time, all presses continuously for twice.The process program table as shown in Figure 7.
Handle tolerance and reach 8000Nm
3/ h.H
2Yield＞98%, CO in the product hydrogen and nitrogen gas
2≤ 0.2%.
Embodiment 3:
The device of embodiment 1 is increased by three towers, form a cover nine tower apparatus, valve 6,7,8 connects each desorb pipeline respectively, and valve 9,10,11 is positioned on each desorb pipeline.Working procedure is seen Fig. 4.Adsorption tower is pressed A, D, G, and B, E, H and C, F, I are divided into three groups, see Fig. 3.With first group be example, when the A tower vacuumizes, valve 9 opens, valve 6 and valve 8 cuts out, after the A tower finishes to vacuumize, valve 9 cuts out, valve 6 is opened, and assists the B tower to vacuumize.After the B tower was taken out true end, valve 8 left by shut off valve 6, assisted the C tower to vacuumize until the D tower and began to vacuumize shut off valve 8, open valve 9.Other tower is the same with the step that the A tower vacuumizes, and just staggers mutually on the time.This device is a raw material with conversion gas, and other condition and embodiment 1 are same, and motor is 220KWh/h altogether.Device is handled tolerance 12000Nm
3/ h, hydrogen yield 99%, CO in the hydrogen and nitrogen gas
2≤ 0.2%.
Claims (7)
1, a kind of multi-tower pressure-changeable gas-adsorption separation method, the cycle period of each tower all includes absorption (A), drop pressure (ED), wash or vacuumize (VC) along venting, boost pressure (ER), (FR) step of finally boosting, each tower along venting flushing or vacuumize step continuously or overlap, each tower is connected with the desorb pipeline by sequencing valve, the number that is in the tower of adsorbed state by synchronization divides into groups adsorption tower, evacuation step in every group of adsorption tower is discontinuous, and every group of adsorption tower connects one tunnel desorb pipeline and vavuum pump.
2, multi-tower pressure-changeable gas-adsorption separation method according to claim 1 is characterized in that connecting with sequencing valve between the desorb pipeline, on the desorb pipeline sequencing valve is arranged.
3, multi-tower pressure-changeable gas-adsorption separation method according to claim 2 is characterized in that the number that synchronization is in the tower of adsorbed state is 2.
4, multi-tower pressure-changeable gas-adsorption separation method according to claim 2 is characterized in that the number that synchronization is in the tower of adsorbed state is 3.
5,, it is characterized in that in drop pressure and suitable venting flushing or vacuumize having between the step forward or the reverse pressure step of putting according to claim 1 or 2 or 3 or 4 described multi-tower pressure-changeable gas-adsorption separation methods.
6, multi-tower pressure-changeable gas-adsorption separation method according to claim 5, it is characterized in that each tower forward or reverse putting press step (D) and vacuumize (VC) or carry out simultaneously by different desorb pipelines along the rinsing step of exitting.
7,, it is characterized in that to increase isolation step after each step according to claim 1 or 2 or 3 or 4 described multi-tower pressure-changeable gas-adsorption separation methods.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96117584A CN1089621C (en) | 1996-06-10 | 1996-06-10 | Multi-tower pressure-changeable gas-adsorption separation method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96117584A CN1089621C (en) | 1996-06-10 | 1996-06-10 | Multi-tower pressure-changeable gas-adsorption separation method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1146369A CN1146369A (en) | 1997-04-02 |
| CN1089621C true CN1089621C (en) | 2002-08-28 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN96117584A Expired - Fee Related CN1089621C (en) | 1996-06-10 | 1996-06-10 | Multi-tower pressure-changeable gas-adsorption separation method |
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Families Citing this family (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1298410C (en) * | 2005-02-01 | 2007-02-07 | 四川天一科技股份有限公司 | Pressure varying adsorption with two downflow releasing tanks |
| CN101549241B (en) * | 2009-05-01 | 2011-09-07 | 宇星科技发展(深圳)有限公司 | Pressure swing adsorption recovery unit of organic exhaust gas |
| CN101817715B (en) * | 2009-08-06 | 2013-06-26 | 四川亚连科技有限责任公司 | Method for extracting methane gas from marsh gas |
| CN102278303A (en) * | 2010-06-10 | 2011-12-14 | 镇江江大泵业科技有限公司 | Double-sealing pressure reducing device for marine long shaft pumps |
| CN104656618B (en) * | 2015-01-19 | 2017-05-31 | 河南心连心化肥有限公司 | Pressure-variable adsorption agent regenerating control device and its control method |
| CN105233624B (en) * | 2015-10-21 | 2018-03-02 | 中国石油化工股份有限公司 | A kind of organic gas processing unit and its application method based on absorption with pressure |
| CN110124446B (en) * | 2019-06-11 | 2023-06-06 | 成都益志科技有限责任公司 | Pressure swing adsorption gas separation system and separation method for improving desorption effect without energy consumption |
| CN112275089A (en) * | 2020-10-15 | 2021-01-29 | 河南中烟工业有限责任公司 | Effluent disposal polluted gas purification system |
| 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 |
| CN113477031A (en) * | 2021-06-18 | 2021-10-08 | 四川亚联高科技股份有限公司 | Pressure swing adsorption device and control method thereof |
| CN114471082B (en) * | 2021-12-27 | 2023-11-24 | 昆山欧拓气体设备有限公司 | Energy-saving VPSA oxygen production method and equipment |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3986849A (en) * | 1975-11-07 | 1976-10-19 | Union Carbide Corporation | Selective adsorption process |
| CN1069708A (en) * | 1991-08-24 | 1993-03-10 | 化学工业部西南化工研究院 | From ammonia factory conversion gas, remove the pressure swing adsorption technique of carbonic acid gas |
| CN1162500A (en) * | 1996-02-29 | 1997-10-22 | 普拉塞尔技术有限公司 | Large capacity vacuum pressure swing adsorption process and system |
-
1996
- 1996-06-10 CN CN96117584A patent/CN1089621C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3986849A (en) * | 1975-11-07 | 1976-10-19 | Union Carbide Corporation | Selective adsorption process |
| CN1069708A (en) * | 1991-08-24 | 1993-03-10 | 化学工业部西南化工研究院 | From ammonia factory conversion gas, remove the pressure swing adsorption technique of carbonic acid gas |
| CN1162500A (en) * | 1996-02-29 | 1997-10-22 | 普拉塞尔技术有限公司 | Large capacity vacuum pressure swing adsorption process and system |
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| Publication number | Publication date |
|---|---|
| CN1146369A (en) | 1997-04-02 |
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