CN105586089A - A method of recovering C2 and higher hydrocarbons by utilizing a VPSA technique - Google Patents
A method of recovering C2 and higher hydrocarbons by utilizing a VPSA technique Download PDFInfo
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Abstract
A method of recovering C2 and higher hydrocarbons by utilizing a VPSA technique is disclosed. The method includes 1) a step of feeding raw material gas into a first adsorption bed group the inside of which is loaded with an adsorbent, performing vacuum pressure swing adsorption for separation to obtain product gas A, and directly discharging the raw material gas that is not adsorbed or weakly adsorbed and is adopted as vent gas, and 2) a step of feeding the product gas A in the step 1) into a second adsorption bed group the inside of which is loaded with an adsorbent, and performing vacuum pressure swing adsorption for separation to obtain product gas B, wherein one part of the product gas B is returned, combined with the product gas A and fed into the second adsorption bed group again, the other part of the product gas B is adopted as product gas and is recovered and reutilized, the product gas A that is not adsorbed or weakly adsorbed is returned, combined with the raw material gas and fed into the first adsorption bed group again, and both the first adsorption bed group and the second adsorption bed group comprise six adsorption beds. The mole ratio of the C2 and higher hydrocarbons in the product gas recovered through the method is 92% or above, and the recovery rate of the C2 and higher hydrocarbons is 95% or above.
Description
Technical field
The present invention relates to a kind of method that the VPSA of utilization technology reclaims C2 and above hydro carbons thereof, particularly oneKind utilize VPSA technical point from reclaiming tail gas that polypropylene factory or polyethylene factory discharge and both gaseous mixtures,Obtain the method for the gas product of high concentration C2 and above hydro carbons thereof.
Background technology
In polypropylene factory (or device) and polyethylene factory (or device) production process, can discharge a large amount of tail gas, itsBe divided in polypropylene factory (or device) and polyethylene factory (or device) production process and discharge torch gas and polypropyleneFactory's (or device) and polyethylene factory (or device) powder degassing cabin powder kills the tail gas of generation time alive, polypropylene factoryWherein some is to follow to produce in (or device) and polyethylene factory (or device) production process, to discharge torch gasThe discharge of journey continous-stable, some is equipment leakage, and some is safety valve emptying discharge, and some is deviceMaterial balance operation fluctuation discharge, some is accident or shutting down emptying discharge, in tail gas, main component isHydrogen, nitrogen, methane, ethene, ethane, propylene, propane, butane, butylene and ethane, thereby, tail gasMain component be taking hydrocarbon gas as main, directly discharge not only causes the waste of hydro carbons environment also to be produced simultaneouslyAdverse effect, thus need to further recycle it.
Mainly contain compression condensation method, Deep Cooling Method, film recovery for the exhaust gas treating method that contains hydrocarbon gas at presentMethod, absorption method etc. Compression condensation method is the temperature by reducing gas or the pressure that increases gas, makes hydrocarbonClass arrives hypersaturated state, and hydrocarbon component condensation is got off, and the method is applicable to the situation that hydro carbons concentration ratio is higher,And the rate of recovery is lower. Deep Cooling Method refers to the hydro carbons of the condensation temperature gas recovery below approximately-100 DEG C, oftenNeed cryogen refrigeration method and turbine expansion restraining cold process to combine, complex technical process, and be applicable to atm numberSituation. Film absorption method is to utilize film preferentially to permeate the characteristic of hydro carbons, by hydrocarbon component enrichment, and then combinationThe methods such as condensation are recycled hydro carbons, although the method further improves the rate of recovery of hydro carbons, and for reclaiming profitProvide new method with nitrogen, but the performance difference of diffusion barrier is larger, cannot industrial standardization.
Absorption method is to utilize specific area adsorbent very large, loose structure to carry out the hydro carbons in adsorbed gas, normalWith adsorbent be active carbon and hydrophobic zeolite adsorbent, be applicable to the situation that handle hydrocarbon concentration ratio is lower,At present the more of use is Vacuum Pressure Swing Adsorption, but and current absorption method is conventionally used in single covering device or overlaps moreOn the device of same process, the rate of recovery of the product obtaining and purity are not high, are unfavorable for the entering of hydro carbons reclaimingOne step utilization.
Summary of the invention
A kind of method that object of the present invention provides the VPSA of utilization technology to reclaim C2 and above hydro carbons thereof, the method structureThink ingenious, flow process is simple, can effectively improve the rate of recovery of C2 and above hydro carbons thereof and the method for purity.
Technical scheme of the present invention is such: a kind of VPSA of utilization technology recovery C2 and above hydro carbons thereofMethod, specifically comprises the following steps:
1) unstripped gas is sent into the first adsorbent bed group that inside is filled with adsorbent and is carried out Vacuum Pressure Swing Adsorption separation,Gas product A, be not adsorbed or the unstripped gas of weak absorption is directly discharged as discharge gas;
2) by step 1) in gas product A send into the second adsorbent bed group that inside is filled with adsorbent and carry out verySpace-variant is pressed adsorbing separation, obtains gas product B, and a described gas product B part is returned and is incorporated to gas product A and again entersEnter the second adsorbent bed group, another part carries out recycling as gas product, be not adsorbed or weak absorptionGas product A returns to be incorporated to and in unstripped gas, again enters the first adsorbent bed group.
Described the first adsorbent bed group and the second adsorbent bed group include 6 adsorbent beds.
Step 1) and step 2) in every adsorbent bed experience successively absorption, all pressure drops, vacuumize, and all pressStep rises and finally boosts.
The method of above-mentioned recovery C2 and above hydro carbons thereof adopts two sections of VPSA extracting and concentrating technologies, and first unstripped gas passes throughFirst paragraph VPSA concentrate obtains C2And the gas product A of the concentration of above hydro carbons about 50mol%, middle producingProduct gas A process second segment VPSA is further by C in gas product2And the concentration of above hydro carbons is brought up to 92mol%Above; In this technique due to unstripped gas is carried out to concentrate twice, and the row who separates in second segment VPSAVenting is directly discharge not, reclaims, thereby make second segment VSPA but be incorporated to first paragraph VPSA entranceIn do not have C2And the loss of above hydro carbons, thereby in making to reclaim the purity of C2 and above hydrocarbon products gas thereof andThe rate of recovery is improved widely. On the other hand, because the gas product B part reclaiming is returned and is incorporated to gas product AIn again experience second segment VPSA, purity and the rate of recovery of C2 and above hydro carbons thereof in the gas product that makes to reclaimBe further enhanced.
Detailed process is as follows:
First paragraph VPSA extracting and concentrating technology
1-1) adsorption process
Under normal pressure, unstripped gas is through the adsorbent bed in the first adsorbent bed group, wherein C2And above hydro carbons is by specialAbsorb with adsorbent, be not adsorbed or methane, the N of weak absorption2、H2Discharge gas directly from inhaling Deng conductAttached bed outlet is discharged. As the C being adsorbed2And the mass-transfer zone forward position of above hydro carbons (being called absorption forward position) arrives and inhalesWhen attached bed outlet, turn off inlet valve and the outlet valve of the unstripped gas of this adsorbent bed, stop absorption.
1-2) equal pressure drop process
After adsorption process finishes, adsorbent bed internal pressure reduces gradually along absorption direction, and forward Exhaust Gas is usedIn the first adsorbent bed group, other has completed the boosting of adsorbent bed of vacuum regeneration process, through 2 equal pressure dropsCheng Hou, the methane in adsorbent bed, N2、H2Significantly reduce Deng gas, C2 and above hydro carbons concentration thereof are able toImprove.
1-3). vacuum
After all pressure drop finishes, for adsorbent is regenerated thoroughly, use vavuum pump against adsorbing direction to absorptionBed vacuumizes, and further reduces adsorbent bed internal pressure to vacuum state (0.09MPa-0.03MPa),The hydrocarbon component of absorption is thoroughly desorbed, and Vacuum solutions is air-breathing is gas product A;
1-4). all voltage rise processes
After vacuum regeneration process completes, use from other adsorbent bed row in equal pressure drop in the first adsorbent bed groupThe gas going out boosts to adsorbent bed, and after 2 equal voltage rise processes, the pressure of adsorbent bed approaches once moreAdsorptive pressure.
1-5). the process of finally boosting
After boost pressure process completes, by boosting, adsorbent bed pressure is risen to adsorption pressure by control valve discharge gasPower.
Second segment VPSA extracting and concentrating technology
2-1). adsorption process
Gas product A is sent under normal pressure to the adsorbent bed of the second adsorbent bed group, C wherein2And above hydro carbons quiltAdsorbent absorbs, and is not adsorbed or methane, the N of weak absorption2、H2Return and be incorporated to raw material Deng gas product AIn gas, again send in the first adsorbent bed group. As the C being adsorbed2And the mass-transfer zone forward position of above hydro carbons (is calledAbsorption forward position) arrive bed when outlet, turn off inlet valve and the outlet valve of the gas product A of this adsorbent bed, stop inhalingAttached.
2-2). drop pressure process
After adsorption process finishes, adsorbent bed internal pressure reduces gradually along absorption direction, and forward Exhaust Gas is usedIn the second adsorbent bed group, other has completed the boosting of adsorbent bed of vacuum regeneration process, all presses by continuous 2 timesProcess, the gas such as H2, N2, CH4 in adsorbent bed significantly reduces, and C2 and above hydro carbons concentration thereof are carriedHigh.
2-3) vacuum
After all pressure finishes, for adsorbent is regenerated thoroughly, use vavuum pump against adsorbing direction to adsorbent bedLayer vacuumizes, and further reduces adsorbent bed internal pressure to vacuum state (0.09MPa-0.03MPa), makesThe hydrocarbon component of absorption is thoroughly desorbed, and Vacuum solutions is air-breathing is gas product B. A gas product B part is returnedBe incorporated in gas product A and again send in the second adsorbent bed group, another part reclaims and carries out as gas productUtilize.
2-4) boost pressure process
After vacuum regeneration process completes, use from other adsorbent bed row in equal pressure drop in the second adsorbent bed groupThe gas going out boosts to adsorbent bed, and after 2 pressure equalizings, the pressure of adsorbent bed once more approaches and inhalesEnclosure pressure.
2-5) the process of finally boosting
After all voltage rise process completes, by boosting, adsorbent bed pressure is risen to adsorptive pressure by control valve discharge gas.
The first adsorbent bed group of the present invention and the second adsorbent bed group comprise six adsorbent bed groups, the first absorptionSix adsorbent bed groups of bed group represent with adsorbent bed A1, B1, C1, D1, E1, F1 respectively, the second adsorbent bed groupSix adsorbent beds represent with adsorbent bed A2, B2, C2, D2, E2, F2 respectively, six of the first adsorbent bed groupThe Vacuum Pressure Swing Adsorption sequential of adsorbent bed in an adsorption cycle is as shown in table 1, six of the second adsorbent bed groupVacuum Pressure Swing Adsorption sequential in adsorption cycle of adsorbent bed is as shown in table 2, and wherein A represents absorption, E1D tableShow an equal step-down, E2D represents two equal step-downs, and V represents to vacuumize, and 0 represents not work (wait): E2R representsTwo all boost, and E1R represents that one all boosts, and FR represents final rise.
Any time, there is an adsorbent bed carrying out absorption work, 6 suctions of the first or second adsorbent bed groupIn attached bed when the state of any one adsorbent bed in equal pressure drop, in corresponding adsorbent bed group, all have one otherThe state of adsorbent bed in equal voltage rise.
Table 1 the first adsorbent bed group Vacuum Pressure Swing Adsorption sequential
| Step order | 1 | 2 | 3 | 4 | 5 | 6 | 7 | 8 | 9 | 10 | 11 | 12 |
| A1 | A | A | E1D | E2D | V | V | V | V | 0 | E2R | E1R | FR |
| B1 | 0 | E2R | E1R | FR | A | A | E1D | E2D | V | V | V | V |
| C1 | V | V | V | V | 0 | E2R | E1R | FR | A | A | E1D | E2D |
| D1 | E1R | FR | A | A | E1D | E2D | V | V | V | V | 0 | E2R |
| E1 | V | V | 0 | E2R | E1R | FR | A | A | E1D | E2D | V | V |
| F1 | E1D | E2D | V | V | V | V | 0 | E2R | E1R | FR | A | A |
Table 2 the second adsorbent bed group Vacuum Pressure Swing Adsorption sequential
| Step order | 1 | 2 | 3 | 4 | 5 | 6 | 7 | 8 | 9 | 10 | 11 | 12 |
| A2 | A | A | E1D | E2D | V | V | V | V | 0 | E2R | E1R | FR |
| B2 | 0 | E2R | E1R | FR | A | A | E1D | E2D | V | V | V | V |
| C2 | V | V | V | V | 0 | E2R | E1R | FR | A | A | E1D | E2D |
| D2 | E1R | FR | A | A | E1D | E2D | V | V | V | V | 0 | E2R |
| E2 | V | V | 0 | E2R | E1R | FR | A | A | E1D | E2D | V | V |
| F2 | E1D | E2D | V | V | V | V | 0 | E2R | E1R | FR | A | A |
The tail gas that described unstripped gas discharges for polypropylene factory or polyethylene factory or both gaseous mixtures.
The tail gas that polyethylene factory discharges is divided into high pressure exhaust gas and low-pressure tail gas, and the tail gas that polypropylene factory discharges isLow-pressure tail gas, described low-pressure tail gas need be pressurized to the pressure of high pressure exhaust gas, has realized like this different pressures gradeUnstripped gas pressure rating before entering retracting device consistent, ensured the stability of exhaust gas recovery system.
Step 1) and step 2) described in adsorbent by A-AS alumina adsorbant, HXSI-01 silica gel inhaleAttached dose and HX-X adsorbent of molecular sieve composition, its mass percent is respectively: A-AS alumina adsorbant1.7-3.7%, HXSI-01 silica gel absorber 89.3-94.3%, HX-X adsorbent of molecular sieve 4-6%. , this adsorbentAdsorption capacity, intensity is large, regenerability good, has improved the pure of C2 in the gas product reclaiming and above hydro carbons thereofDegree and the rate of recovery.
In order further to reduce to adsorb dead space, improve the rate of recovery of C2 and above hydro carbons thereof, described absorptionAgent type of feed in adsorbent bed adopts dense phase loading.
Beneficial effect: the present invention is simple to operate, invest low, make reclaim gas product in C2 and above hydrocarbon thereofThe summation of class shared mol ratio in gas product is greater than 92%, C2 and the above hydro carbons rate of recovery is greater than 95%,Thereby the gas product reclaiming can, after overcompression, separating, directly return in polyethylene and polypropylene production apparatusRow further utilizes; In addition, the concentration of the C2 in exhaust emissions gas and above hydro carbons thereof is by before treatment15-20mol% is reduced to 1mol% left and right, has effectively controlled the discharge of hydrocarbon gas, has reduced hydro carbons through torchThe carbon dioxide that burning produces, has effectively protected atmospheric environment.
Embodiment
In each moment, each adsorbent bed is carrying out the different Vacuum Pressure Swing Adsorption operational phases, each absorptionBed comprises absorption, all pressure drops, vacuumizes, equal voltage rise and the process of finally boosting, and embodiment 1-5 is with adsorbent bed A1With A2 be that example is narrated, the low-pressure tail gas that the low-pressure tail gas described in table 3-table 7 kind discharges for polypropylene factory andThe mixed air of the low-pressure tail gas that polyethylene factory discharges, the high pressure exhaust gas that high pressure exhaust gas discharges for polyethylene factory.The high pressure exhaust gas that wherein polyethylene factory discharges refers to that polyethylene factory powder degassing cabin powder kills the tail producing time aliveGas (polyethylene factory powder degassing cabin powder kill the tail gas producing time alive before going out device by defeated after compressor boostBring, so be high pressure exhaust gas with respect to torch gas, polypropylene factory powder degassing cabin powder degassing cabin),The low-pressure tail gas that polypropylene factory discharges refers to the torch gas and the polypropylene that in polypropylene factory production process, dischargeFactory's powder degassing cabin powder kills the tail gas producing time alive, and the low-pressure tail gas that polyethylene factory discharges is that polyethylene factory is rawThe torch gas discharging in product process.
Embodiment 1
The low-pressure tail gas (pressure of low-pressure tail gas is 2-5KPa) that polypropylene factory and polyethylene factory discharge mixes(in low-pressure tail gas, the main component of C2 and above hydro carbons thereof and main component thereof are shared in low-pressure tail gas afterwardsMol ratio is as shown in table 3) boost to 15-25KPa through blower fan, then the high pressure exhaust gas discharging with polyethylene factory(pressure of low-pressure tail gas is 15-25KPa, the main component of C2 and above hydro carbons thereof and master thereof in high pressure exhaust gasWant composition shared mol ratio mol ratio in high pressure exhaust gas as shown in table 3) be mixed together rear as raw material pneumatic transmissionEnter by A1 bed and carry out Vacuum Pressure Swing Adsorption separation, its technological process comprises absorption, all pressure drops, vacuumizes, allVoltage rise and the process of finally boosting, obtain gas product A, be not adsorbed or the unstripped gas of weak absorption as discharge gas quiltDirectly discharge, gas product A again enters A2 bed and carries out Vacuum Pressure Swing Adsorption separation, and its technological process is wrapped equallyDraw together absorption, all pressure drops, vacuumize, all voltage rise and the process of finally boosting, the gas product B obtaining, the product of gainedA product gas B part is returned and is incorporated to gas product A and again enters the second adsorbent bed group, and another part is as reclaimingGas product stores and further utilizes, and is not adsorbed or the gas product A of weak absorption returns and is incorporated in unstripped gasThe inferior first adsorbent bed group that enters. As shown in table 3, in the gas product reclaiming, C2 and above hydro carbons thereof is mainComposition is ethene, ethane, propylene, propane, butane, butylene and hexane, wherein ethene, ethane, propylene,Propane, butane, butylene and hexane shared mol ratio in gas product is respectively 0.22%, 5.49%, 12.98%,34.29%, 34.79%, 1.71%, 3.28%, 2.49%, shared the rubbing in gas product of C2 and above hydro carbons thereofEr Bida 95.25%, the rate of recovery of gas product reaches 97.2%,, C2 and above hydro carbons thereof in the discharge gas being dischargedIn discharge gas, shared mol ratio only has 0.71%,
This pressure-swing absorption process adsorbent is by A-AS alumina adsorbant, HXSI-01 silica gel absorber and HX-XAdsorbent of molecular sieve composition, its mass percent is respectively: A-AS alumina adsorbant 2.7%, HXSI-01 siliconGlue adsorbent 92.3%, HX-X adsorbent of molecular sieve 5%, adsorbent type of feed in adsorbent bed adopts close phaseFilling.
Table 3
Embodiment 2
The low-pressure tail gas (pressure of low-pressure tail gas is 2-5KPa) that polypropylene factory and polyethylene factory discharge mixes(in low-pressure tail gas, the main component of C2 and above hydro carbons thereof and main component thereof are shared in low-pressure tail gas afterwardsMol ratio is as shown in table 4) boost to 15-25KPa through blower fan, then the high pressure exhaust gas discharging with polyethylene factory(pressure of low-pressure tail gas is 15-25KPa, the main component of C2 and above hydro carbons thereof and master thereof in high pressure exhaust gasWant composition shared mol ratio mol ratio in high pressure exhaust gas as shown in table 4) be mixed together rear as raw material pneumatic transmissionEnter by A1 bed and carry out Vacuum Pressure Swing Adsorption separation, its technological process comprises absorption, all pressure drops, vacuumizes, allVoltage rise and the process of finally boosting, obtain gas product A, be not adsorbed or the unstripped gas A of weak absorption as discharge gasDirectly discharged, gas product A again enters A2 bed and carries out Vacuum Pressure Swing Adsorption separation, and its technological process is sameComprise absorption, all pressure drops, vacuumize, all voltage rise and the process of finally boosting, the gas product B obtaining, gainedA gas product B part is returned and is incorporated to gas product A and again enters the second adsorbent bed group, and another part is as recoveryGas product store and further utilize, be not adsorbed or the gas product A of weak absorption returns and is incorporated in unstripped gasAgain enter the first adsorbent bed group. As shown in table 4, the master of C2 and above hydro carbons thereof in the gas product reclaimingWanting composition is ethene, ethane, propylene, propane, butane, butylene and hexane, wherein ethene, ethane, propylene,Propane, butane, butylene and hexane shared mol ratio in gas product is respectively 0.22%, 5.49%, 12.98%,34.29%, 34.79%, 1.71%, 3.28%, 2.49%, shared the rubbing in gas product of C2 and above hydro carbons thereofEr Bida 95.25%, the rate of recovery of gas product reaches 97.2%,, C2 and above hydro carbons thereof in the discharge gas being dischargedIn discharge gas, shared mol ratio only has 0.71%,
This pressure-swing absorption process adsorbent is by A-AS alumina adsorbant, HXSI-01 silica gel absorber and HX-XAdsorbent of molecular sieve composition, its mass percent is respectively: A-AS alumina adsorbant 1.7%, HXSI-01 siliconGlue adsorbent 94.3%, HX-X adsorbent of molecular sieve 4%, adsorbent type of feed in adsorbent bed adopts close phaseFilling.
Table 4
Embodiment 3
The low-pressure tail gas (pressure of low-pressure tail gas is 2-5KPa) that polypropylene factory and polyethylene factory discharge mixes(in low-pressure tail gas, the main component of C2 and above hydro carbons thereof and main component thereof are shared in low-pressure tail gas afterwardsMol ratio is as shown in table 5) boost to 15-25KPa through blower fan, then the high pressure exhaust gas discharging with polyethylene factory(pressure of low-pressure tail gas is 15-25KPa, the main component of C2 and above hydro carbons thereof and master thereof in high pressure exhaust gasWant composition shared mol ratio mol ratio in high pressure exhaust gas as shown in table 5) be mixed together rear as raw material pneumatic transmissionEnter by A1 bed and carry out Vacuum Pressure Swing Adsorption separation, its technological process comprises absorption, all pressure drops, vacuumizes, allVoltage rise and the process of finally boosting, obtain gas product A, be not adsorbed or the unstripped gas of weak absorption as discharge gas quiltDirectly discharge; The gas product A of gained again enters A2 bed and carries out Vacuum Pressure Swing Adsorption separation, its technological processComprise equally absorption, all pressure drops, vacuumize, all voltage rise and the process of finally boosting, the gas product B obtaining, instituteA gas product B part return and be incorporated to gas product A and again enter the second adsorbent bed group, another part conductThe gas product reclaiming stores and further utilizes, and is not adsorbed or the gas product A of weak absorption returns and is incorporated to raw materialIn gas, again enter the first adsorbent bed group. As shown in table 5, C2 and above hydro carbons thereof in the gas product reclaimingMain component be ethene, ethane, propylene, propane, butane, butylene and hexane, wherein ethene, ethane,Propylene, propane, butane, butylene and hexane shared mol ratio in gas product is respectively 1.07%, 4.15%,14.26%, 34.13%, 33.36%, 1.13%, 1.67%, 2.24%, the summation of C2 and above hydro carbons thereof is being producedMol ratio shared in product gas reaches 92.01%, and the rate of recovery of gas product reaches 97.4%, and in the discharge gas being dischargedC2 and above hydro carbons thereof shared mol ratio in discharge gas only has 0.85%,
This pressure-swing absorption process adsorbent is by A-AS alumina adsorbant, and HXSI-01 silica gel absorber and HX-X divideSub-sieve adsorbant composition, its mass percent is respectively: A-AS alumina adsorbant 3.7%, HXSI-01 silica gelAdsorbent 89.3%, HX-X adsorbent of molecular sieve 6%, adsorbent type of feed in adsorbent bed adopts close dress mutuallyFill out.
Table 5
Embodiment 4
The low-pressure tail gas (pressure of low-pressure tail gas is 2-5KPa) that polypropylene factory and polyethylene factory discharge mixes(in low-pressure tail gas, the main component of C2 and above hydro carbons thereof and main component thereof are shared in low-pressure tail gas afterwardsMol ratio is as shown in table 6) boost to 15-25KPa through blower fan, then the high pressure exhaust gas discharging with polyethylene factory(pressure of low-pressure tail gas is 15-25KPa, the main component of C2 and above hydro carbons thereof and master thereof in high pressure exhaust gasWant composition shared mol ratio mol ratio in high pressure exhaust gas as shown in table 6) be mixed together rear as raw material pneumatic transmissionEnter by A1 bed and carry out Vacuum Pressure Swing Adsorption separation, its technological process comprises absorption, all pressure drops, vacuumizes, allVoltage rise and the process of finally boosting, obtain gas product A, be not adsorbed or the unstripped gas of weak absorption as discharge gas quiltDirectly discharge, gas product A again enters A2 bed and carries out Vacuum Pressure Swing Adsorption separation, and its technological process is wrapped equallyDraw together absorption, all pressure drops, vacuumize, all voltage rise and the process of finally boosting, the gas product B obtaining, the product of gainedA product gas B part is returned and is incorporated to gas product A and again enters the second adsorbent bed group, and another part is as reclaimingGas product stores and further utilizes, and is not adsorbed or the gas product A of weak absorption returns and is incorporated in unstripped gasThe inferior first adsorbent bed group that enters. As shown in table 6, in the gas product reclaiming, C2 and above hydro carbons thereof is mainComposition is ethene, ethane, propylene, propane, butane, butylene and hexane, wherein ethene, ethane, propylene,Propane, butane, butylene and hexane shared mol ratio in gas product is respectively 1.64%, 4.18%, 12.25%,35.13%, 33.96%, 1.21%, 1.99%, 1.96%, shared the rubbing in gas product of C2 and above hydro carbons thereofEr Bida 92.26%, the rate of recovery of gas product reaches 96%, and in the discharge gas being discharged, C2 and above hydro carbons thereof existIn discharge gas, shared mol ratio only has 0.85%.
In this pressure-swing absorption process, adsorbent is by A-AS alumina adsorbant, HXSI-01 silica gel absorber and HX-XAdsorbent of molecular sieve composition, its mass percent is respectively: A-AS alumina adsorbant 2.7%, HXSI-01 siliconGlue adsorbent 92.3%, HX-X adsorbent of molecular sieve 5%, adsorbent type of feed in adsorbent bed adopts close phaseFilling.
Table 6
Embodiment 5
The low-pressure tail gas (pressure of low-pressure tail gas is 2-5KPa) that polypropylene factory and polyethylene factory discharge mixes(in low-pressure tail gas, the main component of C2 and above hydro carbons thereof and main component thereof are shared in low-pressure tail gas afterwardsMol ratio is as shown in table 7) boost to 15-25KPa through blower fan, then the high pressure exhaust gas discharging with polyethylene factory(pressure of low-pressure tail gas is 15-25KPa, the main component of C2 and above hydro carbons thereof and master thereof in high pressure exhaust gasWant composition shared mol ratio mol ratio in high pressure exhaust gas as shown in table 7) be mixed together rear as raw material pneumatic transmissionEnter by A1 bed and carry out Vacuum Pressure Swing Adsorption separation, its technological process comprises absorption, all pressure drops, vacuumizes, allVoltage rise and the process of finally boosting, obtain gas product A, be not adsorbed or the unstripped gas of weak absorption as discharge gas quiltDirectly discharge; The gas product A of gained again enters A2 bed and carries out Vacuum Pressure Swing Adsorption separation, and its technological process is sameSample comprises absorption, all pressure drops, vacuumizes, all voltage rise and the process of finally boosting, the gas product B obtaining, gainedA gas product B part return and be incorporated to gas product A and again enter the second adsorbent bed group, another part is as returningThe gas product of receiving stores and further utilizes, and is not adsorbed or the gas product A of weak absorption returns and is incorporated to unstripped gasIn again to enter the first adsorbent bed group as shown in table 7, the master of C2 and above hydro carbons thereof in the gas product reclaimingWanting composition is ethene, ethane, propylene, propane, butane, butylene and hexane, wherein ethene, ethane, propylene,Propane, butane, butylene and hexane shared mol ratio in gas product is respectively 0.13%, 4.78%, 7.22%,23.92%, 51.82%, 1.87%, 3.75%, 3.25%, C2 and above hydro carbons thereof shared in gas productMol ratio reaches 96.74%, and the rate of recovery of gas product reaches 96.5%, and in the discharge gas being discharged C2 and more thanHydro carbons shared mol ratio in discharge gas only has 1.05%,
In this pressure-swing absorption process, adsorbent is by A-AS alumina adsorbant, HXSI-01 silica gel absorber and HX-XAdsorbent of molecular sieve composition, its mass percent is respectively: A-AS alumina adsorbant 2.7%, HXSI-01 siliconGlue adsorbent 92.3%, HX-X adsorbent of molecular sieve 5%, adsorbent type of feed in adsorbent bed adopts close phaseFilling.
Table 7
Claims (6)
1. utilize VPSA technology to reclaim a method for C2 and above hydro carbons thereof, specifically comprise the following steps:
1) unstripped gas is sent into the first adsorbent bed group that inside is filled with adsorbent and is carried out Vacuum Pressure Swing Adsorption separation,Gas product A, be not adsorbed or the unstripped gas of weak absorption is directly discharged as discharge gas;
2) by step 1) in gas product A send into the second adsorbent bed group that inside is filled with adsorbent and carry out verySpace-variant is pressed adsorbing separation, obtains gas product B, and a described gas product B part is returned and is incorporated to gas product A and again entersEnter the second adsorbent bed group, another part carries out recycling as gas product, is not adsorbed or the product of weak absorptionProduct gas A returns to be incorporated to and in unstripped gas, again enters the first adsorbent bed group;
Described the first adsorbent bed group and the second adsorbent bed group include six adsorbent beds.
2. the method for utilizing VPSA technology to reclaim C2 and above hydro carbons thereof according to claim 1, itsBe characterised in that step 1) and step 2) in every adsorbent bed experience successively absorption, all pressure drops, vacuumize,All voltage rise and steps of finally boosting.
3. the method for utilizing VPSA to reclaim C2 and above hydro carbons thereof according to claim 1, its featureBe the tail gas that described unstripped gas discharges for polypropylene factory or polyethylene factory or both gaseous mixtures.
4. the method for utilizing VPSA to reclaim C2 and above hydro carbons thereof according to claim 3, its featureBe, the tail gas that polyethylene factory discharges is divided into high pressure exhaust gas and low-pressure tail gas, the tail gas that polypropylene factory dischargesFor low-pressure tail gas, described low-pressure tail gas need be pressurized to the pressure of high pressure exhaust gas.
5. the method for utilizing VPSA to reclaim C2 and above hydro carbons thereof according to claim 1, its featureBe step 1) and step 2) described in adsorbent by A-AS alumina adsorbant, HXSI-01 silica gelAdsorbent and HX-X adsorbent of molecular sieve composition, its mass percent is respectively: A-AS alumina adsorbant1.7-3.7%, HXSI-01 silica gel absorber 89.3-94.3%, HX-X adsorbent of molecular sieve 4-6%.
6. the method for utilizing VPSA to reclaim C2 and above hydro carbons thereof according to claim 5, its featureBe step 1) and step 2) described in adsorbent in adsorbent bed type of feed adopt dense phase loading.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106693609A (en) * | 2017-01-20 | 2017-05-24 | 上海华西化工科技有限公司 | Method for recovering tail gas of ethylene-propylene device |
| CN107774095A (en) * | 2016-08-25 | 2018-03-09 | 四川天采科技有限责任公司 | A kind of natural gas is dehydrated the full temperature journey pressure swing adsorption purge method of de- hydrocarbon simultaneously |
| CN107789949A (en) * | 2016-08-30 | 2018-03-13 | 四川天采科技有限责任公司 | A kind of gas separating method of negative pressure pressure-variable adsorption |
| CN107961644A (en) * | 2016-10-20 | 2018-04-27 | 中国石油化工股份有限公司 | A kind of system and method for harmless treatment broken coal low-temperature methanol washing tail-gas |
| CN110180322A (en) * | 2019-06-05 | 2019-08-30 | 杨皓 | A kind of technique obtaining highly concentrated unsaturated component mixed gas from off-gas |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1330974A (en) * | 2000-06-28 | 2002-01-16 | 四川天一科技股份有限公司 | Vacuum pressure-variable process for removing ethane or hydrocarbons over ethane from gas-state hydrocarbon |
| US6517611B1 (en) * | 2001-07-23 | 2003-02-11 | Engelhard Corporation | Olefin separations employing CTS molecular sieves |
| CN1555905A (en) * | 2004-01-07 | 2004-12-22 | 扬子石油化工股份有限公司 | Method of recovering ethylene by pressure swing adsorption |
| CN104059692A (en) * | 2014-05-23 | 2014-09-24 | 四川天采科技有限责任公司 | Method for recovering hydrogen, C2 and fraction light dydrocarbon in combination manner |
-
2014
- 2014-10-22 CN CN201410568826.8A patent/CN105586089B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1330974A (en) * | 2000-06-28 | 2002-01-16 | 四川天一科技股份有限公司 | Vacuum pressure-variable process for removing ethane or hydrocarbons over ethane from gas-state hydrocarbon |
| US6517611B1 (en) * | 2001-07-23 | 2003-02-11 | Engelhard Corporation | Olefin separations employing CTS molecular sieves |
| CN1555905A (en) * | 2004-01-07 | 2004-12-22 | 扬子石油化工股份有限公司 | Method of recovering ethylene by pressure swing adsorption |
| CN104059692A (en) * | 2014-05-23 | 2014-09-24 | 四川天采科技有限责任公司 | Method for recovering hydrogen, C2 and fraction light dydrocarbon in combination manner |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107774095A (en) * | 2016-08-25 | 2018-03-09 | 四川天采科技有限责任公司 | A kind of natural gas is dehydrated the full temperature journey pressure swing adsorption purge method of de- hydrocarbon simultaneously |
| CN107774095B (en) * | 2016-08-25 | 2020-06-02 | 四川天采科技有限责任公司 | Full-temperature-range pressure swing adsorption purification method for simultaneously dehydrating and dealkylating natural gas |
| CN107789949A (en) * | 2016-08-30 | 2018-03-13 | 四川天采科技有限责任公司 | A kind of gas separating method of negative pressure pressure-variable adsorption |
| CN107961644A (en) * | 2016-10-20 | 2018-04-27 | 中国石油化工股份有限公司 | A kind of system and method for harmless treatment broken coal low-temperature methanol washing tail-gas |
| CN106693609A (en) * | 2017-01-20 | 2017-05-24 | 上海华西化工科技有限公司 | Method for recovering tail gas of ethylene-propylene device |
| CN110180322A (en) * | 2019-06-05 | 2019-08-30 | 杨皓 | A kind of technique obtaining highly concentrated unsaturated component mixed gas from off-gas |
| CN110180322B (en) * | 2019-06-05 | 2022-02-22 | 杨皓 | Process for obtaining high-concentration unsaturated component mixed gas from purge gas |
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