CN110354637A - A kind of method of the easy adsorbed gas of pressure swing adsorption method enrichment - Google Patents
A kind of method of the easy adsorbed gas of pressure swing adsorption method enrichment Download PDFInfo
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- 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
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Abstract
The present invention provides a kind of methods of easy adsorbed gas of pressure swing adsorption method enrichment, which comprises (1) unstripped gas enters the first adsorption tower, carries out adsorption operations to adsorbent and reaches saturation；(2) the first adsorption tower after absorption is subjected to equal press operation；(3) product gas is passed through and unadsorbed gas is replaced, the gas displaced is purged into other adsorption towers；(4) the first adsorption tower after displacement is subjected to equal press operation again；(5) the first adsorption tower is subjected to vacuum desorption, obtains product gas；(6) the first adsorption tower after desorption is subjected to pressurising.The present invention cooperates multiple adsorption towers using above-mentioned operation, realize the enrichment of easy adsorbed gas, especially using product gas as displacement gas, and the gas displaced is made to enter other adsorption towers, equal press operation is carried out after displacement, replacement result is not only improved, the concentration and the rate of recovery of easy absorbed component also can be improved.
Description
Technical field
The invention belongs to gas-adsorption technique fields, are related to a kind of method of easy adsorbed gas of pressure swing adsorption method enrichment, especially
A kind of method of its easy adsorbed gas of pressure swing adsorption method enrichment for being related to displacement containing product gas.
Background technique
Pressure-variable adsorption is common a kind of gas separate mode in chemical industry, due to its strong flexibility, operating cost it is low,
The advantages such as separating effect is good obtain extensive industrial application.The gas easily adsorbed can be recycled after adsorbing separation as needed,
Residual gas of difficult absorption, or both can be recycled while being recycled.Wherein, adsorbent be influence separating effect factor it
One, the design optimization of adsorption process is equally most important to the promotion of separating effect.
Currently, the step of process of gas absorption separation generally comprises absorption, presses, desorbs, fills eventually, and replacing is also to inhale
Commonly one of operation in attached process, when can be used for improving product design to a certain extent, but carrying out replacement operator, absorption
For gas in tower in addition to there are also portioned product gas for impurity gas, the gas direct emission after displacement will cause the damage of target product gas
Lose, reduce product recovery rate while may also result in pollution, and if the gas after displacement is transmitted back to head tank, can reduce
The gas treatment amount of adsorbent.In addition, generally being replaced using low pressure when carrying out gas separation under high pressure, low pressure displacement
Operate it is not only limited to the enrichment effect of product gas, but also can due to partial pressures of target gases reduction and lead to gas desorption, instead
And reduce the treating capacity and enrichment effect of object gas.
CN 107694284A discloses a kind of method of multitower displacement Vacuum Pressure Swing Adsorption concentration coal gas layer methane, mainly
Including pressurization, CH4Absorption, CO2Displacement, decompression, adsorbent vacuum desorption, vacuum purging and etc., this method displacement before does not use
The pressure of equal press operation, displacement gas is higher, can both replace the unadsorbed gas in tower, can also replace methane, gas is caused to separate
It is ineffective, and use CO2Other impurities gas can also be introduced by being replaced, and the enrichment of methane in coal bed gas is unfavorable for.CN
102350171A discloses a kind of gas separating method using substitute mode, shares at least six adsorption tower common combination and realizes
Circulation absorption, each adsorption tower is sequentially completed absorption, decompression, emptying, replaces, vacuumizes, boosting and the circulating process of pressurising,
In the same time, each adsorption tower completes a process, but this method is that the impurity aspiration in unstripped gas is attached, and as base
Plinth completes subsequent handling, it is preferred that emphasis is gas separation operational sequence and each is inhaled for absorption and the case where enrichment product gas
The mated condition of attached tower has bigger difference.
In conclusion the enrichment of separation and easy adsorbed gas for component in mixed gas, it is also necessary to seek more excellent
The process of change, sufficiently to improve the concentration and the rate of recovery of product gas.
Summary of the invention
In view of the problems of the existing technology, the purpose of the present invention is to provide a kind of easy adsorbed gas of pressure swing adsorption method enrichment
The method of body, the method that the present invention uses pressure-variable adsorption, the selective absorption using adsorbent to target components make gas absorption
The gas displaced in separation process enters other adsorption towers, and equal press operation is used after displacement, in enhancing replacement result
Meanwhile greatly improving the concentration and the rate of recovery of product gas.
To achieve this purpose, the present invention adopts the following technical scheme:
The present invention provides a kind of methods of easy adsorbed gas of pressure swing adsorption method enrichment, the described method comprises the following steps:
(1) unstripped gas enters the first adsorption tower, and easy absorbed component therein is adsorbed by adsorbent, difficult absorbed component outflow,
Adsorption operations carry out to adsorbent reaching saturation；
(2) by the first adsorption tower and the equal press operation of third adsorption tower progress after step (1) absorption；
(3) product gas is passed through the first adsorption tower after step (2) is pressed, unadsorbed gas is replaced, will be replaced
Gas purging out enters step in the third adsorption tower of (2)；
(4) by the first adsorption tower and the equal press operation of the 4th adsorption tower progress after step (3) displacement；
(5) the first adsorption tower after pressing step (4) vacuumizes, the easy absorbed component solution adsorbed through step (1)
It inhales, obtains product gas；
(6) gas and foreign gas for being displaced the first adsorption tower after step (5) desorption using the 4th adsorption tower are carried out
Pressurising carries out step (1) operation again.
In the present invention, a set of absorption process is completed in selective absorption using adsorbent to target components in adsorption tower,
After the easy absorbed component absorption in unstripped gas, it is depressured by equal press operation, then the unadsorbed gas in displacement sorption tower, sets
The gas to swap out then enters in other adsorption towers being arranged in parallel, then the step of passing through the pressure after displacement, vacuum desorption, is mentioning
While high product gas purity, the rate of recovery of product gas also can be improved；The gas that other adsorption towers displace is re-introduced into after desorption
Pressurization and final pressurising further increase the rate of recovery of easy adsorbed gas, complete whole operation process, and then circulation carries out.
It is used as currently preferred technical solution below, but not as the limitation of technical solution provided by the invention, passes through
Following technical scheme can preferably reach and realize technical purpose and beneficial effect of the invention.
As currently preferred technical solution, the method needs at least five adsorption tower to complete circulation absorption.
Preferably, completed in each adsorption tower it is described absorption, press, replace, press, desorb, pressurising the step of.
In the present invention, according to the operational sequence in each adsorption tower and the disengaging relationship of gas between adsorption tower, at least
5 adsorption towers are arranged in parallel, during an adsorption tower can be made to complete an operating process, other adsorption towers can be never
It sets out with node, a circulation can be equally completed with identical sequence, realizes the mutual cooperation of multiple adsorption towers, improve former
Expect the processing speed of gas.
In the present invention, " first ", " third " " the 4th " before adsorption tower etc. only carry out area to the adsorption tower being arranged in parallel
Point, and the differentiation mode is not fixation, it is different in step (2) when being such as the first adsorption tower with one of adsorption tower
Surely it can only be pressed with third adsorption tower, be the correspondence in process, the first adsorption tower needs to be depressured, and another proceeds to solution
The adsorption tower for process of boosting after suction then conforms exactly to require, and is not limited to third adsorption tower, i.e. synchronization, different absorption
Tower is in the different phase in sorption cycle, and respectively not identical, the rank of operational sequence in the quantity and sorption cycle of adsorption tower
Section division numbers are related；Focus on process between multiple adsorption towers in the present invention to match, makes it that can be completed at the same time one
A circulation absorption.
As currently preferred technical solution, step (1) described unstripped gas includes easy absorbed component and difficult absorbed component,
Wherein easy absorbed component includes methane.
Preferably, in the unstripped gas easy absorbed component volume fraction be 2~60%, such as 2%, 5%, 10%,
20%, 30%, 40%, 50% or 60% etc., it is not limited to cited numerical value, other are unlisted in the numberical range
Numerical value is equally applicable.
Preferably, the difficult absorbed component includes any one in nitrogen, oxygen, carbon monoxide or inert gas or at least
Two kinds of combination, the combination is typical but non-limiting example has: the group of the combination of nitrogen and oxygen, oxygen and carbon monoxide
It closes, nitrogen, carbon monoxide and combination of inert gas etc..
In the present invention accessible unstripped gas need to meet specific adsorbent have to the adsorptivity of different component it is obvious poor
Not, to utilize the strong adsorptivity separation and purification to easy absorbed component.Methane is easy absorption group in the unstripped gas that the present invention is handled
Point, including middle low concentration coal-bed gas, industrial Methane offgas etc..
In step (1) of the present invention, unstripped gas enters from absorption tower bottom, and easy absorbed component is enriched in adsorption tower, adsorbs
Methane concentration bottom first increases in tower, and then top increases again, is equivalent to methane concentration distribution curve front end and constantly moves up, in real time
The methane concentration at adsorption column outlet is measured, shows that adsorbent bed starts to penetrate when starting to obviously increase, stopping is passed through unstripped gas.
As currently preferred technical solution, step (1) described adsorbent includes active carbon, molecular sieve or ionic liquid boiling
Any one in stone or at least two combination, the combination is typical but non-limiting example has: the group of active carbon and molecular sieve
It closes, the combination of molecular sieve and ionic liquid zeolite, active carbon, molecular sieve and combination of ionic liquid zeolite etc., preferably ionic liquid boiling
Stone.
As currently preferred technical solution, step (1) adsorptive pressure be 0.1~1.0MPa, such as 0.1MPa,
0.2MPa, 0.3MPa, 0.4MPa, 0.5MPa, 0.6MPa, 0.8MPa or 1.0MPa etc., it is not limited to cited numerical value,
Other unlisted numerical value are equally applicable in the numberical range.
In the present invention, the selection of adsorptive pressure mainly by absorbed component concentration easy in unstripped gas depending on, and ought wherein contain
When ignitable components, such as methane, oxygen content can determine its explosion limit, be considered based on safety, and adsorptive pressure is also by oxygen content
It influences.
It in the present invention, when methane concentration is lower in unstripped gas, is generally preferred with atmospheric operation, guarantees safety, methane is dense
When spending higher, pressurized operation can be used, stripping process ability is improved.
Preferably, step (1) adsorption temp is -10~60 DEG C, such as -10 DEG C, 0 DEG C, 10 DEG C, 20 DEG C, 30 DEG C, 40
DEG C, 50 DEG C or 60 DEG C etc., it is not limited to cited numerical value, other unlisted numerical value are equally suitable in the numberical range
With preferably 20~30 DEG C.
As currently preferred technical solution, step (2) and step (4) the equal press operation are independently at least one
Grade.
In the present invention, step (1) complete absorption after absorption tower pressure interior force it is higher, be connected to the adsorption tower of other low-pressures into
Row pressure balance, foreign gas and a small amount of unadsorbed methane enter another adsorption tower, and methane caused by being expelled directly out is avoided to return
Yield reduces；It arbitrarily downgrades several, is determined according to the displacement pressure of next step.
Preferably, step (3) the displacement pressure be 80~1000kPa, such as 80kPa, 100kPa, 150kPa,
200kPa, 300kPa, 400kPa, 500kPa, 600kPa, 800kPa or 1000kPa etc., it is not limited to cited number
Value, other interior unlisted numerical value of the numberical range are equally applicable.
There are still unabsorbed gases in adsorption tower after in the present invention, adsorbing, pressing, using product gas to unadsorbed gas
It is replaced, methane partial pressure is higher in product gas, and the foreign gas solution of adsorbent surface will be adsorbed on by the Effect of Competitive Adsorption
It inhales, enters another adsorption tower for needing to boost in company with unadsorbed gas purging, and methane-gas scale is very big in this adsorption tower
Improve, at the same reduce as methane gas flow directly out and caused by the rate of recovery be lost, time swap product gas as needed
Middle methane concentration and the rate of recovery and adjust.
Preferably, the pressure 5~100kPa low compared with displacement pressure after step (2) and step (4) are pressed, such as 5kPa,
10kPa, 20kPa, 30kPa, 40kPa, 50kPa, 60kPa, 80kPa or 100kPa etc., it is not limited to cited numerical value,
Other unlisted numerical value are equally applicable in the numberical range.
In the present invention, adsorption tower is higher using pressure after product gas displacement, can also carry out equal press operation, reduce tower pressure, keep away
It is higher to exempt from energy consumption needed for desorption phase, can also discharge part foreign gas, with improve desorption obtain the purity of methane.
As currently preferred technical solution, step (5) is described vacuumize after, the first absorption tower pressure interior force is 10~
35kPa, such as 10kPa, 15kPa, 20kPa, 25kPa, 30kPa or 35kPa etc., it is not limited to cited numerical value, it should
Other unlisted numerical value are equally applicable in numberical range.
In the present invention, adsorption tower is vacuum-treated using vacuum pump, wherein adsorbed gas is desorbed, and is realized simultaneously
The regeneration of adsorbent.
If not the pressure each means absolute pressure in addition, specially referring in the present invention.
Preferably, after step (5) desorption, the first adsorption tower first carries out equal press operation.
Preferably, the equal press operation is at least level-one, it is preferred to use third adsorption tower and the 4th adsorption tower are successively pressed.
Preferably, after the equal press operation, the pressure in the first adsorption tower is lower than displacement 5~100kPa of pressure, such as
5kPa, 10kPa, 20kPa, 30kPa, 40kPa, 50kPa, 60kPa, 80kPa or 100kPa etc., it is not limited to cited
Numerical value, other interior unlisted numerical value of the numberical range are equally applicable.
In the present invention, adsorption column pressure is lower after vacuum desorption, needs to carry out pressurising, to avoid the need for excessive foreign gas,
It first can also be pressed using the cooperation between adsorption tower, the gas containing a small amount of methane is introduced while improving pressure, be improved
Methane recovery.
As currently preferred technical solution, after the gas pressurized that step (6) uses the 4th adsorption tower to displace, also wrap
Include equal press operation again.
In the present invention, there are replacement operators after adsorption tower absorption, and the gas purged out enters other and needs absorption of boosting
Tower, therefore, when this adsorption tower proceeds to boost phase, according to the cooperation between adsorption tower, the same time has carry out replacement operator
Adsorption tower, its purge gas is introduced into this adsorption tower, further increases tower pressure, transfer of the gas between each adsorption tower facilitates
The raising of methane recovery；It, can be again if still differing larger with adsorptive pressure after introducing the gas that other adsorption towers displace
It is secondary to be pressed, it is however generally that, the two is not much different.
As currently preferred technical solution, step (6) described foreign gas includes purified gas and/or unstripped gas, preferably
For purified gas.
Preferably, pressure with step (1) adsorptive pressure of the foreign gas are identical.
Preferably, the purified gas carries out reversed pressurising, opposite with the flow direction of raw material in step (1).
Preferably, the purified gas includes nitrogen and oxygen, the difficult absorption group that adsorption operations are discharged preferably in step (1)
Point.
In the present invention, in circulation absorption process finally, be finally pressurized to adsorptive pressure using gas, start the cycle over again
It is adsorbed, tower bottom is generally preferentially blown to from tower top to the reversed pressurising of adsorption tower using purified gas, it can be with compressed methane concentration
Distribution curve improves the methane treating capacity of unit volume adsorbent.
As currently preferred technical solution, the described method comprises the following steps:
(1) unstripped gas enters the first adsorption tower, and easy absorbed component therein is adsorbed by adsorbent, difficult absorbed component outflow,
Adsorption operations carry out to adsorbent reaching saturation, and the adsorptive pressure is 0.1~1.0MPa, and adsorption temp is -10~60 DEG C；
(2) pressure ratio by the first adsorption tower and the equal press operation of third adsorption tower progress after step (1) absorption, after pressing
Step (3) replaces the low 5~100kPa of pressure；
(3) product gas is passed through the first adsorption tower after step (2) is pressed, unadsorbed gas is replaced, it is described to set
Changing pressure is 80~1000kPa, and the gas displaced purging is entered step in the third adsorption tower of (2)；
(4) pressure ratio by the first adsorption tower and the equal press operation of the 4th adsorption tower progress after step (3) displacement, after pressing
Step (3) replaces the low 5~100kPa of pressure；
(5) the first adsorption tower after pressing step (4) carries out being evacuated to pressure being 10~35kPa, inhales through step (1)
Attached easy absorbed component desorption, obtains product gas；
(6) the first adsorption tower after step (5) desorption is successively pressed with third adsorption tower and the 4th adsorption tower；
(7) gas and foreign gas that the first adsorption tower after pressing step (6) is displaced using the 4th adsorption tower carry out
The pressure of pressurising, foreign gas is identical as step (1) adsorptive pressure, then carries out step (1) operation again.
Compared with prior art, the invention has the following advantages:
(1) the method for the invention is pressed to adsorb, is replaced, pressing, desorbing, the process of pressurising realizes easy adsorbed gas
Enrichment, especially using product gas as displacement gas, and make the gas displaced enter other adsorption towers, not only improve displacement effect
The concentration and the rate of recovery of easy absorbed component also can be improved in fruit；
(2) equal press operation is carried out after present invention displacement, the concentration of foreign gas in adsorption tower can be further decreased, to mention
The concentration of methane in high product gas；The energy consumption in vacuum desorption operating process is reduced by reducing the pressure of adsorption tower；
(3) multiple adsorption tower cooperations in the method for the invention, are shifted by the gas between each tower, avoid unadsorbed mesh
Mark component is expelled directly out, and improves product recovery rate, and multiple adsorption towers operate the processing speed that unstripped gas can be improved simultaneously.
Detailed description of the invention
Fig. 1 is the adsorbent equipment structure connection diagram that the embodiment of the present invention 1 provides；
Fig. 2 is the operating process schematic diagram for the adsorbent equipment that the embodiment of the present invention 1 provides；
Fig. 3 is the adsorbent equipment structure connection diagram that the embodiment of the present invention 2 provides；
Wherein, the first adsorption tower of 101A-, the second adsorption tower of 101B-, 101C- third adsorption tower, the 4th adsorption tower of 101D-,
The 5th adsorption tower of 101E-, 201- product gas storage device.
Specific embodiment
In order to better illustrate the present invention, it is easy to understand technical solution of the present invention, below further specifically to the present invention
Bright but following embodiment is only simple example of the invention, does not represent or limit the scope of the present invention, this hair
Bright protection scope is subject to claims.
The following are typical but non-limiting embodiments of the invention:
Embodiment 1:
A kind of method for present embodiments providing pressure swing adsorption method enrichment methane, what the method was arranged in parallel using 5
Adsorption tower group at device operated, the structure connection diagram of described device is as shown in Figure 1, include the first adsorption tower
101A, the second adsorption tower 101B, third adsorption tower 101C, the 4th adsorption tower 101D and the 5th adsorption tower 101E further include charging
Line, displacement line, desorption line, fills line at cable bond eventually, and every pipeline is independently connected with 5 adsorption towers, and is equipped with valve；Displacement
Line and desorption line are connected with product gas storage device 201.
The present embodiment illustrates the operational sequence of enrichment methane by taking 5 tower operating processes as an example；The adsorption pressure wherein used
Power is 120kPa, desorption pressures 20kPa, by taking the first adsorption tower 101A as an example, including 20 step operating processes, it is respectively as follows: 1. suctions
It is attached；2. absorption；3. absorption, 4. absorption；5. vacant；6. pressing；7. displacement；8. vacant；9. pressing；10. vacant；11. vacant；
12. vacant；13. desorption；14. desorption；15. desorption；16. desorption；17. pressing；18. pressing；19. importing the gas displaced；
20. filling eventually；Other adsorption towers carry out 20 step circulations according to same sequence, different nodes respectively, and the operating process of described device is shown
It is intended to as shown in Fig. 2, being operated by the number order of process.
Below by taking the first adsorption tower 101A as an example, 20 step operating processes are illustrated:
1-4. absorption: opening valve 101A and 102A, and unstripped gas enters the first adsorption tower 101A, and contacts with adsorbent,
Adsorptive pressure is 120kPa, wherein easy absorbed component methane is enriched in adsorption tower, difficult absorbed component, such as N2、O2And CO,
Tail gas tank is flowed out to from tower top, the methane concentration at real-time measurement adsorption column outlet stops being passed through original after adsorbent adsorption saturation
Expect gas.
5. vacant: closing valve 101A and 102A, do not carry out any operation to the first adsorption tower 101A, pressure is maintained at
120kPa。
6. pressing: opening valve 104A and 104C, the first adsorption tower 101A of connection and third adsorption tower 101C, inhaled to first
Attached tower 101A carries out pressure release, and third adsorption tower 101C boosts, and the pressure of two towers is 92kPa after pressing.
7. displacement: open valve KV13, using product gas (105kPa) to unadsorbed gas in the first adsorption tower 101A into
Line replacement is purged and enters third adsorption tower 101C, and displacement gas methane partial pressure is higher, will be adsorbed on the impurity of adsorbent surface
Gas desorption purges out tower in turn.
8. vacant: closing valve 104A, 104C and KV13, do not carry out any operation to the first adsorption tower 101A, pressure is protected
It holds in 105kPa.
9. pressing: opening valve 104A and 104D, be connected to the first adsorption tower 101A and the 4th adsorption tower 101D, inhaled to first
Attached tower 101A carries out pressure release, and the 4th adsorption tower 101D boosts, and two pressure towers are 65kPa after pressing.
10-12. is vacant: closing valve 104A and 104D, does not carry out any operation to the first adsorption tower 101A, pressure is kept
In 65kPa.
13-16. desorption: opening valve 108A, is connected to the first adsorption tower 101A and vacuum pump, to the first adsorption tower 101A into
Row vacuum pumping, the methane product purified simultaneously regenerate adsorbent, and desorption vacuum degree is 20kPa.
17. pressing: closing valve 108A, open valve 104A and 104C, the first adsorption tower 101A of connection and third are adsorbed
Tower 101C is pressurized the first adsorption tower 101A, and third adsorption tower 101C carries out pressure release, and the pressure of two towers is after pressing
65kPa。
18. pressing: valve 104C is closed, valve 104D is opened, is connected to the first adsorption tower 101A and the 4th adsorption tower 101D,
First adsorption tower 101A is pressurized, the 4th adsorption tower 101D carries out pressure release, and two pressure is 92kPa after pressing.
19. importing the gas displaced: valve KV43 is opened, the 4th adsorption tower 101D is replaced using product gas,
The gas displaced purges to the first adsorption tower 101A, the first adsorption tower 101A and is further pressurized to 105kPa.
20. filling eventually: reversely fill eventually to the first adsorption tower 101A using purified gas (120kPa), realize and adsorbed to first
The pressurising of tower 101A starts next circulation.
The enrichment of methane in unstripped gas is carried out, using aforesaid operations process and its operating condition with the original of different methane concentrations
Expect that gas carries out many experiments, three kinds of unstripped gas each component volume fractions are respectively as follows: methane 5.7%, nitrogen 94.3%；Methane
15.6%, nitrogen 84.4%；Methane 25.3%, nitrogen 74.7%.By 30 above-mentioned circulating processes, methane in product gas is measured
The rate of recovery of concentration and methane, the results are shown in Table 1.
The unstripped gas circulation absorption experimental result of different methane concentrations in 1 embodiment 1 of table
Embodiment 2:
A kind of method for present embodiments providing pressure swing adsorption method enrichment methane, what the method was arranged in parallel using 5
Adsorption tower group at device operated, the structure connection diagram of described device is as shown in figure 3, overall structure and connection relationship
Be consistent substantially with embodiment 1, difference is: operation pipe is in addition to including feeding line, cable bond, displacement line, desorption line, end
Line is filled, further includes decompression line.
The present embodiment illustrates the operational sequence of enrichment methane by taking 5 tower operating processes as an example；The adsorption pressure wherein used
Power is 550kPa, desorption pressures 25kPa, by taking the first adsorption tower 101A as an example, including 18 step operating processes, it is respectively as follows: 1. suctions
It is attached；2. absorption；3. absorption, 4. absorption；5. vacant；6. pressing；7. displacement；8. vacant；9. pressing；10. pressing；11. vacant；
12. vacant；13. desorption；14. desorption；15. desorption；16. desorption；17. pressing；18. pressing；19. importing the gas displaced；
20. filling eventually；Other adsorption towers carry out 20 step circulations according to same sequence, different nodes respectively.
Below by taking the first adsorption tower 101A as an example, 20 step operating processes are illustrated:
1-4. absorption: opening valve 101A and 102A, and unstripped gas enters the first adsorption tower 101A, and contacts with adsorbent,
Adsorptive pressure is 550kPa, wherein easy absorbed component methane is enriched in adsorption tower, difficult absorbed component, such as N2、O2And CO,
Tail gas tank is flowed out to from tower top, the methane concentration at real-time measurement adsorption column outlet stops being passed through original after adsorbent adsorption saturation
Expect gas.
5. vacant: closing valve 101A and 102A, do not carry out any operation to the first adsorption tower 101A, pressure is maintained at
550kPa。
6. pressing: opening valve 104A and 104C, the first adsorption tower 101A of connection and third adsorption tower 101C, inhaled to first
Attached tower 101A carries out pressure release, and third adsorption tower 101C boosts, and the pressure of two towers is 390kPa after pressing.
7. displacement: open valve KV13, using product gas (395kPa) to unadsorbed gas in the first adsorption tower 101A into
Line replacement is purged and enters third adsorption tower 101C, and displacement gas methane partial pressure is higher, will be adsorbed on the impurity of adsorbent surface
Gas desorption purges out tower in turn.
8. vacant: closing valve 104A, 104C and KV13, do not carry out any operation to the first adsorption tower 101A, pressure is protected
It holds in 395kPa.
9. pressing: opening valve 104A and 104D, be connected to the first adsorption tower 101A and the 4th adsorption tower 101D, inhaled to first
Attached tower 101A carries out pressure release, and the 4th adsorption tower 101D boosts, and two pressure towers are 220kPa after pressing.
10. pressing: closing valve 104A and 104D, open valve KV14, pressed with vacant surge tank, pressed after pressing
Power is 101kPa.
11-12. is vacant: closing valve KV14, does not carry out any operation to the first adsorption tower 101A, pressure is maintained at
101kPa。
13-16. desorption: opening valve 108A, is connected to the first adsorption tower 101A and vacuum pump, to the first adsorption tower 101A into
Row vacuum pumping, the methane product purified simultaneously regenerate adsorbent, and desorption vacuum degree is 25kPa.
17. pressing: closing valve 108A, open valve 104A and 104C, the first adsorption tower 101A of connection and third are adsorbed
Tower 101C is pressurized the first adsorption tower 101A, and third adsorption tower 101C carries out pressure release, and the pressure of two towers is after pressing
220kPa。
18. pressing: valve 104C is closed, valve 104D is opened, is connected to the first adsorption tower 101A and the 4th adsorption tower 101D,
First adsorption tower 101A is pressurized, the 4th adsorption tower 101D carries out pressure release, and two pressure is 390kPa after pressing.
19. importing the gas displaced: valve KV43 is opened, the 4th adsorption tower 101D is replaced using product gas,
The gas displaced purges to the first adsorption tower 101A, the first adsorption tower 101A and is further pressurized to 395kPa.
20. filling eventually: being carried out using the difficult absorbent components (550kPa) of absorption phase outflow to the first adsorption tower 101A reversed
It fills eventually, realizes the pressurising to the first adsorption tower 101A, start next circulation.
The enrichment of methane in unstripped gas is carried out, using aforesaid operations process and its operating condition with two kinds of different methane concentrations
Unstripped gas tested, in one of mixed gas, each component volume fraction is respectively as follows: methane 40.2%, oxygen
11.6%, nitrogen 48.0% and other gases 0.2%；In another mixed gas, each component volume fraction is respectively as follows: methane
31.1%, oxygen 11.8%, nitrogen 56.8% and other gases 0.3%；By 30 above-mentioned circulating processes, measure in product gas
The rate of recovery of methane concentration and methane, the results are shown in Table 2.
The unstripped gas circulation absorption experimental result of different methane concentrations in 2 embodiment 2 of table
| Experiment numbers | 1 | 2 |
| Methane concentration (%) in unstripped gas | 40.2 | 31.3 |
| Methane concentration (%) in product gas | 99.6 | 96.8 |
| Oxygen concentration (%) in product gas | 0.1 | 0.5 |
| Methane recovery (%) | 97.4 | 96.1 |
Embodiment 3:
A kind of method for present embodiments providing pressure swing adsorption method enrichment methane, what the method was arranged in parallel using 5
Adsorption tower group at device operated, overall structure and connection relationship are consistent substantially with embodiment 1, and difference is: behaviour
Make pipeline in addition to including feeding line, cable bond, displacement line, desorption line, filling line eventually, further includes decompression line.
For the present embodiment by taking 5 tower operating processes as an example, the operational sequence for illustrating enrichment methane is same as Example 2.
Below by taking the first adsorption tower 101A as an example, 20 step operating processes are illustrated:
1-4. absorption: opening valve 101A and 102A, and unstripped gas enters the first adsorption tower 101A, and contacts with adsorbent,
Adsorptive pressure is 950kPa, wherein easy absorbed component methane is enriched in adsorption tower, difficult absorbed component, such as N2、O2And CO,
Tail gas tank is flowed out to from tower top, the methane concentration at real-time measurement adsorption column outlet stops being passed through original after adsorbent adsorption saturation
Expect gas.
5. vacant: closing valve 101A and 102A, do not carry out any operation to the first adsorption tower 101A, pressure is maintained at
950kPa。
6. pressing: opening valve 104A and 104C, the first adsorption tower 101A of connection and third adsorption tower 101C, inhaled to first
Attached tower 101A carries out pressure release, and third adsorption tower 101C boosts, and the pressure of two towers is 699kPa after pressing.
7. displacement: open valve KV13, using product gas (750kPa) to unadsorbed gas in the first adsorption tower 101A into
Line replacement is purged and enters third adsorption tower 101C, and displacement gas methane partial pressure is higher, will be adsorbed on the impurity of adsorbent surface
Gas desorption purges out tower in turn.
8. vacant: closing valve 104A, 104C and KV13, do not carry out any operation to the first adsorption tower 101A, pressure is protected
It holds in 750kPa.
9. pressing: opening valve 104A and 104D, be connected to the first adsorption tower 101A and the 4th adsorption tower 101D, inhaled to first
Attached tower 101A carries out pressure release, and the 4th adsorption tower 101D boosts, and two pressure towers are 408kPa after pressing.
10. pressing: closing valve 104A and 104D, open valve KV14, pressed with vacant surge tank, pressed after pressing
Power is 101kPa.
11-12. is vacant: closing valve KV14, does not carry out any operation to the first adsorption tower 101A, pressure is maintained at
101kPa。
13-16. desorption: opening valve 108A, is connected to the first adsorption tower 101A and vacuum pump, to the first adsorption tower 101A into
Row vacuum pumping, the methane product purified simultaneously regenerate adsorbent, and desorption vacuum degree is 30kPa.
17. pressing: closing valve 108A, open valve 104A and 104C, the first adsorption tower 101A of connection and third are adsorbed
Tower 101C is pressurized the first adsorption tower 101A, and third adsorption tower 101C carries out pressure release, and the pressure of two towers is after pressing
408kPa。
18. pressing: valve 104C is closed, valve 104D is opened, is connected to the first adsorption tower 101A and the 4th adsorption tower 101D,
First adsorption tower 101A is pressurized, the 4th adsorption tower 101D carries out pressure release, and two pressure is 699kPa after pressing.
19. importing the gas displaced: valve KV43 is opened, the 4th adsorption tower 101D is replaced using product gas,
The gas displaced purges to the first adsorption tower 101A, the first adsorption tower 101A and is further pressurized to 750kPa.
20. filling eventually: reversely fill eventually to the first adsorption tower 101A using purified gas (950kPa), realize and adsorbed to first
The pressurising of tower 101A starts next circulation.
The enrichment of methane in unstripped gas is carried out, using aforesaid operations process and its operating condition with two kinds of different methane concentrations
Unstripped gas tested, in one of mixed gas, each component volume fraction is respectively as follows: methane 25.2%, nitrogen
74.8%；In another mixed gas, each component volume fraction is respectively as follows: methane 36.0%, nitrogen 74.0%；By on 30 times
Circulating process is stated, measures the rate of recovery of methane concentration and methane in product gas, the results are shown in Table 3.
The unstripped gas circulation absorption experimental result of different methane concentrations in 3 embodiment 3 of table
| Experiment numbers | 1 | 2 |
| Methane concentration (%) in unstripped gas | 25.2 | 36.0 |
| Methane concentration (%) in product gas | 92.5 | 99.1 |
| Methane recovery (%) | 98.2 | 98.1 |
By embodiment result it is found that the accessible raw material of the present invention wherein methane initial concentration range is wider, in embodiment
Different pressures are used to be adsorbed in safe range for different methane concentrations, when containing oxygen especially in mixed gas,
The selection of adsorptive pressure also needs to consider oxygen content concentration and explosion limit；Methane concentration has controllability, recycling after enrichment
Rate is up to 80% or more, up to 98% or more.
The Applicant declares that the present invention is explained by the above embodiments method detailed of the invention, but the present invention not office
It is limited to the above method, that is, does not mean that the present invention must rely on the above method and could implement.Person of ordinary skill in the field
It will be clearly understood that any improvement in the present invention, to the raw materials used in the present invention, the equivalence replacement of operation and auxiliary material, operation
Addition, the selection etc. of concrete mode, all of which fall within the scope of protection and disclosure of the present invention.
Claims (10)
1. a kind of method of the easy adsorbed gas of pressure swing adsorption method enrichment, which is characterized in that the described method comprises the following steps:
(1) unstripped gas enters the first adsorption tower, and easy absorbed component therein is adsorbed by adsorbent, difficult absorbed component outflow, absorption
Operation carries out reaching saturation to adsorbent；
(2) by the first adsorption tower and the equal press operation of third adsorption tower progress after step (1) absorption；
(3) product gas is passed through the first adsorption tower after step (2) is pressed, unadsorbed gas is replaced, by what is displaced
Gas purging enters step in the third adsorption tower of (2)；
(4) by the first adsorption tower and the equal press operation of the 4th adsorption tower progress after step (3) displacement；
(5) the first adsorption tower after pressing step (4) vacuumizes, and the easy absorbed component through step (1) absorption desorbs, and obtains
To product gas；
(6) gas and foreign gas for displacing the first adsorption tower after step (5) desorption using the 4th adsorption tower carry out pressurising,
Step (1) operation is carried out again.
2. being inhaled the method according to claim 1, wherein the method needs at least five adsorption tower to complete circulation
It is attached；
Preferably, completed in each adsorption tower it is described absorption, press, replace, press, desorb, pressurising the step of.
3. method according to claim 1 or 2, which is characterized in that step (1) described unstripped gas include easy absorbed component and
Difficult absorbed component, wherein easy absorbed component includes methane；
Preferably, the volume fraction of easy absorbed component is 2~60% in the unstripped gas；
Preferably, the difficult absorbed component includes any one in nitrogen, oxygen, carbon monoxide or inert gas or at least two
Combination.
4. method according to claim 1-3, which is characterized in that step (1) described adsorbent include active carbon,
Any one in molecular sieve or ionic liquid zeolite or at least two combination, preferably ionic liquid zeolite.
5. method according to claim 1-4, which is characterized in that step (1) adsorptive pressure be 0.1~
1.0MPa；
Preferably, step (1) adsorption temp is -10~60 DEG C, preferably 20~30 DEG C.
6. method according to claim 1-5, which is characterized in that step (2) and step (4) the equal press operation
Independently at least level-one；
Preferably, step (3) the displacement pressure is 80~1000kPa；
Preferably, the pressure 5~100kPa low compared with displacement pressure after step (2) and step (4) are pressed.
7. method according to claim 1-6, which is characterized in that after being vacuumized described in step (5), the first absorption
Tower pressure interior force is 10~35kPa；
Preferably, after step (5) desorption, the first adsorption tower first carries out equal press operation；
Preferably, the equal press operation is at least level-one, it is preferred to use third adsorption tower and the 4th adsorption tower are successively pressed；
Preferably, after the equal press operation, the pressure in the first adsorption tower is lower than displacement 10~100kPa of pressure.
8. method according to claim 1-7, which is characterized in that step (6) is displaced using the 4th adsorption tower
Gas pressurized after, further include equal press operation again.
9. method according to claim 1-8, which is characterized in that step (6) described foreign gas includes purified gas
And/or unstripped gas, preferably purified gas；
Preferably, pressure with step (1) adsorptive pressure of the foreign gas are identical；
Preferably, the purified gas carries out reversed pressurising, opposite with the flow direction of raw material in step (1)；
Preferably, the purified gas includes nitrogen and oxygen, the difficult absorbed component that adsorption operations are discharged preferably in step (1).
10. -9 described in any item methods according to claim 1, which is characterized in that the described method comprises the following steps:
(1) unstripped gas enters the first adsorption tower, and easy absorbed component therein is adsorbed by adsorbent, difficult absorbed component outflow, absorption
Operation carries out to adsorbent reaching saturation, and the adsorptive pressure is 0.1~1.0MPa, and adsorption temp is -10~60 DEG C；
(2) the pressure ratio step by the first adsorption tower and the equal press operation of third adsorption tower progress after step (1) absorption, after pressing
(3) the low 5~100kPa of displacement pressure；
(3) product gas is passed through the first adsorption tower after step (2) is pressed, unadsorbed gas is replaced, the displacement pressure
Power is 80~1000kPa, and the gas displaced purging is entered step in the third adsorption tower of (2)；
(4) the pressure ratio step by the first adsorption tower and the equal press operation of the 4th adsorption tower progress after step (3) displacement, after pressing
(3) the low 5~100kPa of displacement pressure；
(5) the first adsorption tower after pressing step (4) carries out being evacuated to pressure being 10~35kPa, through step (1) absorption
Easy absorbed component desorption, obtains product gas；
(6) the first adsorption tower after step (5) desorption is successively pressed with third adsorption tower and the 4th adsorption tower；
(7) gas and foreign gas that the first adsorption tower after pressing step (6) is displaced using the 4th adsorption tower carry out pressurising,
The pressure of foreign gas is identical as step (1) adsorptive pressure, then carries out step (1) operation again.
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