CN85103557B - Methane in the pressure swing adsorption method enrichment coal mine mash gas - Google Patents
Methane in the pressure swing adsorption method enrichment coal mine mash gasInfo
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- CN85103557B CN85103557B CN85103557A CN85103557A CN85103557B CN 85103557 B CN85103557 B CN 85103557B CN 85103557 A CN85103557 A CN 85103557A CN 85103557 A CN85103557 A CN 85103557A CN 85103557 B CN85103557 B CN 85103557B
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Abstract
The present invention provides methane in a kind of pressure swing adsorption method enrichment coal mine mash gas, and it is a kind of pressure swing adsorption method that obtains product gas from desorption phase.For the product gas of production high concentration methane, utilize portioned product gas to reflux in the process and remove to replace bed, to reach the concentration of methane in the further enrichment bed.In order to improve the recovery rate of methane, it is necessary that the discharge gas after the displacement is reclaimed as raw material.Method of the present invention can make low-calorie coal mine mash gas of giving it up be enriched to the methane-rich gas that has high heating value and extensive use is arranged.
Description
The invention relates to and utilize pressure swing adsorption that coal mine mash gas is separated, feasible wherein methane component is able to the method for enrichment.
Coal mine mash gas is the associated gas in colliery, every meter
3Coal can produce 15～30 meters of Device in Gas
3, its typical component following (representing) with percentage by volume:
CH
420-30%
N
250-60%
O
2+Ar 12-18%
H
2O is saturated
Because its calorific value is 1700-2600 kilocalorie/rice only
3About, can't utilize.If can make methane concentration bring up to the 35-50%(volume its enrichment), then its calorific value is about 3000-4300 kilocalorie/rice
3The calorific value level that is equivalent to town gas, can utilize, but methane concentration is limited in this methane rich product gas, often be restricted in industrial application, if can be with more than the methane-rich to 80% in the Device in Gas, to reach the level that is equivalent to heating value of natural gas, promptly calorific value be about 6800-8000 kilocalorie/rice
3, the high methane gas of this high concentration just can be used as the combustion engine fuel of industrial chemicals or automobile.
The object of the invention is to provide that a kind of the coal mine mash gas enrichment to be obtained methane concentration be the 35-96%(volume) the pressure swing absorption process of methane rich product.
Another purpose of the present invention is to provide a kind of pressure swing adsorption method of making high concentration methane product gas and high methane recovery rate.
Other purpose of the present invention will illustrate below.
Well-known pressure swing adsorption method is a kind of the separation from admixture of gas and the technology of Purge gas.Be big with adsorbent adsorption capacity to adsorbate under high pressure (adsorptive pressure), and low pressure (desorption pressures) down adsorption capacity little be characterized as foundation, alternately switch circulation technology by what select that absorption and desorption and regeneration two stages form.The pressure swing adsorption technique of previous development, for example more representative is even pressure type pressure swing adsorption technique of four towers that United States Patent (USP) 3430418 is introduced, their characteristics are to select the absorption phase admixture of gas to pass through bed under adsorptive pressure, wherein the impurity composition is attracted on the adsorbent, obtain product component free from foreign meter in gas phase simultaneously, promptly product component all is the component that is difficult for being adsorbed.The desorption and regeneration stage at first is the direction decompression that the pressure of the tower that stops to adsorb is carried out along absorption, with the product component in the dead space in the further recovery tower all over often being divided into three processes.Then the direction of carrying out against absorption be decompressed to normal pressure and under this pressure with a part of product gas flushing bed, with desorption with remove the impurity composition be adsorbed on the adsorbent.With product gas the tower that flushing finishes is pressurized to adsorptive pressure at last, to prepare to separate once more and purify unstripped gas.Specifically, each tower all must experience absorption, isostasy, seven steps such as decompression, reverse decompression, flushing, a pressurising, secondary pressurising forward.Whole process is to carry out at ambient temperature, and has at least two towers to form pressure swing adsorption systems, and is maximum by ten to 12 systems that tower is formed.What the most generally use is four Tower Systems.This pressure swing adsorption technique purified hydrogen from hydrogen-rich mixture and from air the field of enriched in oxygen most widely used.
Yet the usually used several adsorbents of pressure swing adsorption method to the adsorption capacity of methane in the coal mine mash gas all than other component (dewatering exceptionally) for strong, the product component that obtains is easy absorbed component, and impurity composition is the component that is difficult for being adsorbed, just effect and the implication with typical pressure swing adsorption technique each process in implementation process is opposite fully for this, that is to say what select to adsorb on the absorption phase adsorbent it is product component, what gas phase discharged is that impurity composition is a waste gas, and product component is to obtain in the desorption and regeneration stage, and promptly product component is to obtain mutually from absorption.Another object of the present invention provides and a kind ofly obtains the pressure swing absorption process of product in the desorption and regeneration stage, and enrich methane from coal mine mash gas in this way, to obtain the methane rich product gas of various methane concentrations.
In the pressure swing absorption process enrichment coal mine mash gas basic process of methane be at first absorption phase utilize adsorbent the same adsorptive pressure of environment temperature to Device in Gas in methane different with the adsorption capacity of other component, to absorb by methane (and moisture) in the Device in Gas of bed, and all the other components (as nitrogen, oxygen, argon) that removed methane will be drained from the bed port of export as waste gas.Adsorptive pressure preferably be controlled at the 5-10 kgf/centimetre
2In (gauge pressure) scope.When the absorption forward position of methane moves to the position of a certain regulation of bed, just stop absorption.It then is the desorption section, it at first is airflow direction decompression when absorption, promptly reduce pressure from the tower Way out, its objective is further with in the absorption mutually in the bed also components such as the nitrogen of occlusion, oxygen, argon discharge, to improve the concentration of methane in the bed, till bed layer pressure is reduced to a certain lower pressure, generally be controlled at the 0.5-3 kgf/centimetre
2Between (gauge pressure) pressure, this moment, the absorption forward position of methane was just broken through at the bed port of export.Above-mentioned decompression process is actually two steps of branch and finishes, and at first is pressure equalization step, and it is to utilize the waste gas that discharges in the decompression process pressurising gas as another tower.Next is a depressurization steps forward, contains methane concentration in the waste gas that this step discharged and must be lower than 5%, generally is controlled at the 0.1-3% scope, directly puts then to atmosphere, to guarantee security in the operation process and high methane recovery rate.Behind depressurization steps forward, then utilize a part of methane rich product gas under the pressure of depressurization steps terminal hour forward, to pass through bed from the tower entrance point, and flow out from the tower port of export, this is called displacement step, also can be described as the product reflux step, its objective is with the methane of high adsorption capacity the nitrogen, oxygen, the argon component that still remain in the bed are replaced away, make that methane concentration increases substantially in the bed.Be airflow direction decompression then against when absorption, promptly from the bed importer to decompression, until be close to be substantially equal to atmospheric pressure till, the 0.01-1 kgf that promptly reduces pressure/centimetre
2In the scope of (gauge pressure).This part discharges the part that gas is high concentration methane rich product gas.But this moment is still residual in the bed quite a few methane component, must it be extracted out with vavuum pump, and methane concentration to improve methane concentration in the final product, is the recovery rate that improves methane than higher on the other hand in the gas of extracting out on the one hand.Be to make bed obtain desorb more completely on the one hand again, improved the utilization rate of bed.Reach desorption effect preferably, the vacuum of tower should not be lower than 650 millimetress of mercury.In time forward absorption phase to for the tower that desorb is finished at last, also need to make adsorption tower rise to adsorptive pressure from low pressure, the gas part of pressurising is in the waste gas that pressure weighs and discharges in the tower of equal step from another, and another part is in the waste gas that discharges in the tower of adsorption step from another.Pressurising finishes also to indicate the end in desorption and regeneration stage.Above-mentioned whole process all is under the environment temperature.
The present invention needs two adsorption towers that are loaded with selective absorbent at least, also can be three towers or four towers.The various pressure swing adsorption systems of forming by the tower more than two, wherein must there be a tower to be in the selection absorption phase, other tower then is in the different step in desorption and regeneration stage, they are according to certain rules, carrying out different steps at one time respectively, and the circulation of realization absorption and desorb, product is exported continually.
The used adsorbent of the present invention can be silica gel, aluminium oxide, A type, X type molecular sieve, activated carbon or carbon molecular sieve.To be this adsorbent must be higher than other component in the Device in Gas (it is outer to dewater) to the adsorption capacity of methane to the key issue of selected adsorbent, and especially the separation of methane and nitrogen wants big, simultaneously methane again can be at an easy rate from adsorbent desorption come out.In those adsorbents that transformation absorption is used always, active carbon and carbon molecular sieve can satisfy above-mentioned requirement preferably.
Because the adsorption capacity of moisture on adsorbent is stronger than methane,,, before advancing pressure-swing absorber, should establish the drier that one group of alternating temperature adsorbs in order to obtain dry methane rich product gas so in methane rich product gas, always contain saturation moisture.Drier can be the molecular sieve of silica gel, aluminium oxide or various models.If required methane rich product gas allows to contain saturation moisture, before advancing pressure-swing absorber, can not establish drier so.
Particular content of the present invention is with explanation in more detail below.
Referring to accompanying drawing.Fig. 1 is the schematic diagram of the whole flow process of the present invention.After coal mine mash gas is extracted out from the coal seam, the pressure of 300 millimeters of water is arranged approximately, by pipeline 10, through feed gas compressor 11, be compressed to the 5-10 kgf/centimetre
2(gauge pressure) to separator 13, separates the moisture of separating out in the gas through pipeline 12 there, arrives dryer group 16 through pipeline 15 then.Dryer group 16 can adopt the alternating temperature drier of conventional type.Generally can form the inside filling drier, for example silica gel by two driers.The source of the gas of regeneration drier can adopt the dry waste gas (promptly being equivalent to air) of pressure swing adsorption system output, from pipeline 20 steam heater 21 of flowing through, is heated to about 150 ℃, the drier of the moisture that gone to regenerate saturated.The regeneration off gases of having carried water is put to atmosphere through pipeline 23.
Water content in the dried coal mine mash gas is equivalent to dew point-30～-40 ℃ approximately, and this gas enters pressure swing adsorption system 18 via pipeline 17, concentrates later high concentration methane rich product gas by pipeline 19 outputs.The waste gas that discharges when depressurization steps forward in pressure swing adsorption system is put to atmosphere through pipeline 24.The gas that discharges when displacement step in pressure swing adsorption system because methane concentration is equivalent to the concentration of methane in the coal mine gas in this gas, backflows in feed gas compressor 11 pipeline 10 before by pipeline 25 so can be used as raw material.This is one of characteristics of the present invention, is intended to improve the recovery rate of methane.Feed gas compressor 11 preferably adopts non-lubricated compressor, in order to avoid the oil vapour in the gas pollutes the adsorbent in the pressure-swing absorber.
Fig. 2 is the pressure swing adsorption technique flow chart that is used to implement process of the present invention.Here be illustrated as an example with three-column process flow.This technological process can be applicable to the pressure swing adsorption system 18 among above-mentioned Fig. 1.Illustrate by Fig. 2, three adsorption tower A, B and C that are filled with active carbon or carbon molecular sieve, they be connected in parallel in dried raw material gas house steward 17 and the waste gas header 31 that is not adsorbed between.Automatic valve 26A, 26B and 26C control the unstripped gas charging of adsorption tower A, adsorption tower B and adsorption tower C respectively, and the unstripped gas of indication also is a coal mine mash gas among the present invention.Automatic valve 27A, 27B and 27C control the waste gas that does not contain methane respectively and enter waste gas header 31 from above-mentioned corresponding adsorption tower.
Be adsorbed component and be methane rich product gas by reverse decompression with vacuumize two steps and discharge from the product gas house steward 40 of the entrance point of each adsorption tower. Automatic valve 30A, 30B and 30C will control the gas of discharging from the corresponding column entrance point respectively.The discharge gas of reverse decompression is discharged after automatic valve 41 and pipeline 42 enter into booster compressor 47 pipeline 46 before from house steward 40.Vacuumizing and discharging gas is by vavuum pump 45 it to be extracted out from tower, through product house steward 40, automatic valve 43, vacuum tank 44 and pipeline 46, enters booster compressor 47.Vacuum tank 44 plays the prime vacuum action of vavuum pump 45, and it has made full use of the pumpage of vavuum pump 45 outside vacuumizing step.High concentration methane rich product gas flows to product jar 49 after compression, the pressure of product jar can remain on the 2-8 kgf/centimetre
2(gauge pressure) is by control valve 54 its pressure of control that are contained on the product pipeline 19.High concentration methane rich product gas is finally by pipeline 50, control valve 54 and pipeline 19 output systems.Part high concentration methane rich product advances tower from pipeline 51 backflows, through control valve 52, automatic valve 53 pipeline 40 of flowing through enters one of in automatic valve 30A, 30B and 30C respectively and goes displacement in the corresponding adsorption tower, and the adsorption column pressure during displacement is by control valve 52 controls.After gas after the displacement flows out, enter pipeline 33 one of in automatic valve 29A, 29B and 29C respectively from the port of export of corresponding column, and then through automatic valve 34, valve 35 and pipeline 25, the unstripped gas house steward 10 of backflowing shown in Figure 1.Valve 35 is mainly used in the flow of control displacement gas.
Automatic valve 29A, 29B and 29C also are used for isostasy and the forward decompression between each tower.Forward the discharge gas during depressurization steps is through pipeline 33, automatic valve 36 and valve 37, after pipeline 24 is discharged puts to atmosphere.Valve 37 is mainly used in control and forward reduces pressure and discharge the flow velocity of gas.
Waste gas during absorption is used for the usefulness of the regeneration of drier through waste gas header 31, control valve 32 and pipeline 20.The pressure of adsorption tower when control valve 32 is mainly used in control and keeps absorption.
Automatic valve 28A, 28B and 28C are used for the filling of each pressure tower, and the gas of filling is the waste gas from waste gas header 31, through valve 39 and fill house steward 38 by two and flow to corresponding adsorption tower.Valve 39 is to be used for control inflation flow velocity.
Circulation and time-program(me) referring to table 1 just are more prone to understand implementation process of the present invention.Each adsorbent bed all need experience eight different steps, each step all have the initial sum that flows to (or) terminal.The flow direction of in table 1, having represented all air-flows of relevant three adsorption towers.
By table 1 as seen, each tower is all being carried out mutually different step at one time, at any time, always has an adsorption tower to be in adsorption step, and waste gas is expelled to waste gas header 31 under the situation of pressure substantial constant.Meanwhile an adsorption tower being arranged all the time in other two towers is to use the waste gas pressurising, and the adsorption step that is is subsequently done last preparation, so unstripped gas can successively supply with, rather than intermittently.Meanwhile another tower is experiencing from isostasy to vacuumizing five steps, so the high concentration methane rich product gas of output is to be discharged into product house steward 40 intermittently, but, can guarantee that product gas steady and continuous ground is from pipeline 19 outputs by conventional automatic control and adjustment system.
Be that example illustrates each step that each tower is experienced in once circulating with the A tower now, and participate in the valve that circulation is switched among narration Fig. 2.Also list the residing pressure of adsorption tower in each step.Certainly, in the following description, force value and step time all are to belong to illustrative, can adopt the time of optimal pressure and each step, any restriction never in addition for those in enforcement of the present invention.All valves all are in closed condition before device turns round.
0-6 minute: adsorption step.The A tower 8 kgfs/centimetre
2(gauge pressure) pressure is absorption down.Valve 26A and valve 27A open, dry unstripped gas (coal mine mash gas) 8 kgfs/centimetre
2Flow into A tower arrival ends and by this tower from unstripped gas house steward 17 under (gauge pressure) pressure, the waste gas of being made up of the oxygen that is not adsorbed, argon and nitrogen is from this tower port of export inflow exhaust gas pipeline 31.A part of waste gas carries out second time pressurising by pipeline 38 and valve 28B to the B tower through valve 39 simultaneously.In adsorption step, methane is made this tower arrival end form methane absorption forward position by selectivity absorption (also having adsorbed other component simultaneously on a small quantity), and moves to its port of export gradually.Adsorption step finishes when methane absorption forward position moves in the tower certain certain position.
6-6.5 minute: pressure equalization step.Unstripped gas stops input, and the methane forward position is fully in the A tower.Valve 26A and 27A close.Open valve 29A and valve 29C make between A tower and the C tower and carry out isostasy simultaneously.Just taken out the C tower of vacuum so A tower dead space gas discharges and flows to from this tower port of export, make at last the C pressure tower rise to about 3.5 kgfs/centimetre
2About (gauge pressure) pressure, the methane that be adsorbed in the A tower this moment is moved to the tower port of export by desorption because of step-down, but it is adsorbed not adsorbed the active carbon of methane as yet by the tower port of export, and its absorption forward position does not reach the port of export yet.
6.5-7 minute: depressurization steps forward.When A tower and C pressure tower have reached balance, shut off valve 29C, while open valve 36, the interior gas of A tower dead space is further discharged towards the port of export, i.e. direction decompression of flowing along absorption, the flow velocity that discharges gas is by valve 37 controls, and the A pressure tower further descends, and methane absorption forward position continues to move to the tower port of export because of step-down.When the A pressure tower reduce to 1 kgf/centimetre
2When (gauge pressure), just in time methane absorption forward position is broken through at the tower port of export, and should control methane concentration this moment must be at the 5%(volume) below, otherwise can produce the factor of explosion danger.
7-9 minute: displacement step.When the A tower forward reduces pressure when finishing, promptly shut off valve 36, open valve 53, valve 30A and valve 34, have in the product jar 4 kgfs/centimetre
2The high concentration methane product gas of (gauge pressure) pressure is by pipeline 51, valve 52, reduce to 1 kgf/centimetre
2(gauge pressure) pressure flows into the A tower and goes to replace oxygen, argon and the nitrogen component that still remains in the tower, to reach the effect of further enrich methane.The size of replacement amount is by valve 35 controls, and displacement pressure is by valve 52 controls.Gas after the displacement is through pipeline 25 outputs.
9-9.5 minute: reverse depressurization steps.After displacement step finishes, shut off valve 29A, valve 34, valve 53, open valve 41, enter reverse depressurization steps, interior dead space gas of A tower this moment and the methane component that is adsorbed discharge from the tower entrance point, and through product house steward 40 and pipeline 42, enter pipeline 46, constantly be evacuated to product jar 49 by supercharger 47, methane concentration can reach the 80%(volume in the release gas of this moment) more than, promptly can be used as product gas.
9.5-12 minute: vacuumize step.Reverse decompression finishes when the A pressure tower is reduced to atmospheric pressure, this moment shut off valve 41, open valve 43, A Ta Neishang remains in quite a few methane on the active carbon in product house steward 40 is drawn into the vacuum tank 44 of existing certain vacuum degree rapidly, take away by vavuum pump 45 again, the gas of extracting out is product gas, and wherein methane concentration can reach the 80%(volume) more than.This moment, the vacuum of A tower was the 700(millimetres of mercury).
12-12.5 minute: a pressurising step.The A tower has been finished its absorption, the release of waste gas, the recovery and the desorption process of product.And prepare to begin supercharging successively, at first be to utilize the dead space gas of the B tower of just finishing adsorption step to carry out the pressurising first time.Shut off valve 30A and valve 43, open valve 29A and valve 29B.Because A tower entrance point shuts, continue to flow toward the A tower through pipeline 33 from the dead space gas of B tower, equate until the pressure of two towers, the pressure of this moment be about 3.5 kgfs/centimetre
2About (gauge pressure).
12.5-18 minute: secondary pressurising step.After a pressurising of A tower finished, pressure did not still reach adsorptive pressure, at this moment shut off valve 29A and valve 29B.Open valve 28A utilizes to be in waste gas that adsorption step discharges through valve 39, and 38 pairs of A towers of pipeline carry out pressurising second time, till being substantially equal to adsorptive pressure, at this moment the A pressure tower be about 8 kgfs/centimetre
2(gauge pressure) that is to say that it has finished last supercharging.
The A tower has been finished whole 18 minutes circulation like this, now prepares open valve 26A and valve 27A, adsorbs to import unstripped gas again.The cyclic process of A tower is the representative of all tower A, B, C, and these towers carry out adsorption process in succession with 1/3rd recurrence relation, so that unstripped gas and product gas are successive.In this process, the adsorption step sequence arrangement of tower is A, B, C successively, can certainly be other arrangement scheme such as A, C, B, not what substantial difference here.
Three above-mentioned tower pressure swing adsorption technique flow processs are to implement according to each step of cyclic process of table 1 and time-program(me) table thereof, also can implement according to each step of cyclic process and the time-program(me) table thereof of table 2, table 2 and table 1 difference are to have increased a step between adsorption step and pressure equalization step, be called isolation step, when running to this step, all valve Close Alls that link to each other with this tower, be in closed state, keeping a last state that step is adsorption step terminal hour bed eventually, is that pressure equalization step just finishes when beginning until next procedure.The purpose of arranging this step is in order to adapt to the interior at one time new arrangement mode of carrying out different step between three towers, there is no substantial difference with the arrangement mode of table 1, but such arrangement makes two to fill step and arrange well-to-do not as table 1 in time, can cause thus that tower presses than great fluctuation process, and adopt isolation step also to make the bed utilization rate descend.
Pressure swing adsorption technique flow process of the present invention also can adopt the combining form of two towers or four towers, as shown in Figure 3, Figure 4.Each step of the cyclic process of corresponding flow process and time-program(me) table thereof are shown in table 3, table 4.
The present invention can also discharge reverse decompression in gas and vacuumize and discharge gas and collect respectively, and the former is back in the tower as displacement, and the latter under same operating condition, can obtain better effect like this for product output, but flow process is complicated.
Key problem in technology of the present invention is the desorb means, displacement step is essential when production high concentration methane product gas, and so-called displacement promptly utilizes reverse decompression and vacuumizes in the step part in the collected product and is back to again in the tower that just forward decompression has finished and goes.The ratio that capacity of returns accounts for the said goods amount is referred to as reflux ratio, and reflux ratio is a very important factor in the operation of the present invention, and reflux ratio is big more, and product purity is high more, and utilization ratio of device is low more.Reflux ratio is more little, and product purity is just low more, and utilization ratio of device is just high more.Technology of the present invention can be regulated arbitrarily reflux ratio from 0 to 0.9, produces the methane rich product gas of methane concentration from all size between the 65-95%.
When the reflux ratio when displacement was controlled at 0, methane concentration was about the 50-65%(volume in the product), this situation belongs to a kind of special case of the present invention.According to this situation, when methane concentration in the product only needs to be controlled at the 50-65%(volume) in the scope time, can omit displacement step.
When only producing methane concentration is the 35-50%(volume) methane rich product gas the time, not only can save displacement step, and available rinsing step replaces vacuumizing step, promptly wash to the entrance point direction with being in gas that tower of depressurization steps forward discharges the port of export from the tower that is rinsed, the discharge gas that develops is the part of product gas, above-mentioned situation belongs to another special case of the present invention, and can save vavuum pump this moment.Now briefly explain the process that replaces vacuumizing step with rinsing step with the technological process of Fig. 4 and each step of cyclic process and the time-program(me) thereof of table 4, be example still with the A tower, the A tower was in adsorption step in 0 to 4 minute, continue be in pressure equalization step in 4 to 5 minutes, owing to omitted displacement step, so the time of the forward depressurization steps that comes next can be arranged to 5 to 8 minutes, then be reverse depressurization steps, the time is 8 to 9 minutes; Then be the 9th minute to the 12nd minute again, at this moment should be with rinsing step for it, close automatic valve 36, and open automatic valve 29A, 29D, 30A, 41, use on the occasion of the D tower of depressurization steps forward and discharge gas, through automatic valve 29D and 29A with flushing bed A, gas after the flushing is through automatic valve 30A and pipeline 40, automatic valve 41 and pipeline 42 are transported to pipeline 46, discharge gas with reverse decompression, as exporting after the compressed machine supercharging of product gas.The discharge gas of perhaps reverse decompression and flushing after pipeline 42 directly export, the pressure of the product gas that discharge this moment be the 0.01-1 kgf/centimetre
2In (gauge pressure) scope.
In order to make the present invention's air-flow in implementation process more stable and set up some buffer containers or improve necessary automatic control level and all be fine, do not make generation substantial variation of the present invention.
The three tower pressure swing adsorption technique flow processs of application drawing 2 and each step of circulation and the time sequencing table thereof of table 2, the following test of carrying out can further specify and understand characteristics of the present invention:
Use three adsorption towers, the internal diameter of each tower is 81 millimeters, 800 millimeters of adsorbent floor heights, and interior dress granularity is about 2360 grams of 20～40 purpose active carbons, to select adsorbed methane.
Contain methane 20%(volume) coal mine mash gas be compressed to 8 kgfs/centimetre
2(gauge pressure), temperature is 28 ℃, advances the saturation water that does not remove in advance before the pressure swing adsorption system wherein, its water content is the 0.4%(volume).Unstripped gas is 0.59 mark rice
3/ time, adsorptive pressure be 8 kgfs/centimetre
2(gauge pressure), total cycle time shorten to 12 minutes (comparing with the cycle of table 2), and result of the test is as shown in table 5.
Utilizes and test 1 identical system, but raw material is for containing methane 30.4%(volume) coal mine mash gas, be compressed to 8 kgfs/centimetre
2(gauge pressure) is with 1.1 mark rice
3The flow in/time is just sent into system without preliminary treatment, and temperature is 29 ℃, saves displacement step, and the force value at other each step end is same as test 1.Methane rich product gas is with 0.52 mark rice
3The flow in/time and 0.01 kgf/centimetre
2The pressure output of (gauge pressure), its methane concentration is the 63.9%(volume), the methane recovery rate is 99.4%.
Each step of circulation and the time-program(me) table thereof of the four tower pressure swing adsorption process flow process of application drawing 4 and table 4, the following test of carrying out also can further specify and understand characteristics of the present invention:
Test 3
Use four adsorption towers, the internal diameter of each tower is 81 millimeters, 800 millimeters of adsorbent floor heights, and interior dress granularity is 20～40 purpose active carbons, 3147 grams.
Unstripped gas is for containing methane 29.6%(volume) coal mine mash gas, be compressed to 8 kgfs/centimetre
2(gauge pressure), temperature is 18 ℃, advances the saturation water that does not remove in advance before the pressure swing adsorption system wherein, its water content is the 0.23%(volume) global cycle cycle time is 16 minutes, result of the test is as shown in table 6.
Table 5. production by pressure swing adsorption high concentration methane product result of the test
Table 6. production by pressure swing adsorption low-concentration methane product testing result
Claims (20)
1, the pressure swing adsorption method of separation and enriched gas from admixture of gas, usually form by a series of towers that adsorbent is housed, wherein each tower all must experience adsorb, pressure is all permanent, forward decompression, reverse decompression, flushing, seven steps of a pressurising and secondary pressurising, of the present invention from Device in Gas, separate and each tower of the pressure swing adsorption method of enrich methane all must experience following steps:
A. adsorption step is introduced coal mine mash gas in the pressure swing adsorption system in several adsorption towers that are filled with adsorbent in the tower, and be difficult for being adsorbed component oxygen, argon and nitrogen and discharge from the tower port of export, the component methane and the saturation moisture that easily are adsorbed, occlusion is in tower.
B. the equal homochronous of pressure is rapid, after step a finished, the tower that has adsorbed was connected at the port of export with a certain adsorption tower that has finished to vacuumize step, makes the interior gas of the tower that has adsorbed transport to the adsorption tower that finishes to vacuumize step, till two pressure towers equated, methane component was still stayed in the tower.
C. depressurization steps forward, after step b, the tower that has adsorbed further along the decompression of port of export direction, is just broken through at the port of export until methane component, and tower was pressed and was reduced to an a little higher than atmospheric intermediate pressure this moment.
D. displacement step, under the pressure that forward decompression stops, utilize a part of product gas, pass through to port of export direction from the entrance point of the tower of firm end step e, displacement is fallen a part and is still remained in other component in the tower, and this displacement gas is back in the flow of feed gas goes.
E. reverse depressurization steps after steps d, drains the reverse entrance point from tower of the methane gas that obtains enrichment, and till equal atmospheric pressure, the high methane gas of this part discharge is portioned product gas until the tower pressure drop.
F. vacuumize step, after step e, the tower internal pressure has been atmospheric pressure, but goes back some methane component of occlusion, and this part gas will be extracted it out by vacuumizing, and this moment, tower forced down in atmospheric pressure, and extracting gas out also is the part of product gas.
G. pressurising step, utilize the cat head release gas that does not contain methane of another tower that just has been in pressure equalization step to carry out pressurising to the tower of the above-mentioned f of completing steps, be from the outlet of tower toward the importer to, its pressure is risen to till the pressure of supplying with the source of the gas tower equates.
H. secondary pressurising step: utilize the cat head that does not contain methane of another tower that is in adsorption step to discharge gas and carry out pressurising once more to the tower of the above-mentioned g of completing steps, be from the port of export of tower toward the entrance point direction, its pressure risen to be substantially equal to till the adsorptive pressure.
2, according to the pressure swing adsorption method of claim 1, it is characterized in that: the adsorption tower that needs two filled with adsorbent at least.
3, according to the pressure swing adsorption method of claim 1 and 2, it is characterized in that: being filled with in the adsorption tower has the active carbon of better selection absorption or carbon molecular sieve as adsorbent to methane component.
4, according to the pressure swing adsorption method of claim 1, it is characterized in that: the adsorptive pressure when adsorption step be controlled at 5～10 kgfs/centimetre
2In (gauge pressure) scope.
5, according to the pressure swing adsorption method of claim 1, it is characterized in that: the pressure when depressurization steps forward finishes be controlled at 0.5～3 kgf/centimetre
2In (gauge pressure) scope.
6, according to the pressure swing adsorption method of claim 1, it is characterized in that: the operating pressure of displacement step be controlled at 0.5～3 kgf/centimetre
2In (gauge pressure) scope.
7, according to the pressure swing adsorption method of claim 1, it is characterized in that: the operating pressure when vacuumizing step is not less than vacuum 650 millimetress of mercury.
8, according to the pressure swing adsorption method of claim 1, it is characterized in that: methane concentration must be lower than 5% in the waste gas that is discharged when depressurization steps forward, is controlled at 0.1～3% scope.
9, according to the pressure swing adsorption method of claim 1, it is characterized in that product gas is made up of the exhaust of step e and f, can 2～8 kgfs/centimetre
2(gauge pressure) pressure is output down, perhaps the discharge gas of step e and f is collected respectively, and the former is back in the tower as displacement gas, and the latter exports as product gas.
10, according to the pressure swing adsorption method of claim 1, it is characterized in that displacement gas used in displacement step is the exhaust that comes from step e and f, and compressed machine is compressed to and is greater than or equal to the required pressure of displacement, finally is controlled at displacement and is back in the tower under the required pressure and goes.
11,, it is characterized in that in displacement step reflux ratio is controlled at 0～0.9 scope according to the pressure swing adsorption method of claim 1.
12,, it is characterized in that on the vavuum pump inlet pipeline, establishing a vacuum tank according to the pressure swing adsorption method of claim 1.
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| Application Number | Priority Date | Filing Date | Title |
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| CN85103557A CN85103557B (en) | 1985-04-29 | 1985-04-29 | Methane in the pressure swing adsorption method enrichment coal mine mash gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN85103557A CN85103557B (en) | 1985-04-29 | 1985-04-29 | Methane in the pressure swing adsorption method enrichment coal mine mash gas |
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| Publication Number | Publication Date |
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| CN85103557A CN85103557A (en) | 1986-10-29 |
| CN85103557B true CN85103557B (en) | 1987-10-28 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN85103557A Expired CN85103557B (en) | 1985-04-29 | 1985-04-29 | Methane in the pressure swing adsorption method enrichment coal mine mash gas |
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1985
- 1985-04-29 CN CN85103557A patent/CN85103557B/en not_active Expired
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|---|---|---|---|---|
| CN101100622B (en) * | 2007-07-16 | 2010-12-08 | 张文慧 | Method and device for synthesizing natural gas by using coke oven gas |
| CN101381269B (en) * | 2008-10-14 | 2011-10-05 | 李若彬 | Methane recovery method in coal mine ventilation air methane |
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|---|---|
| CN85103557A (en) | 1986-10-29 |
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