CN1194946C - Pressure swing adsorption method for distilling olefin or ethane from gas mixture - Google Patents
Pressure swing adsorption method for distilling olefin or ethane from gas mixture Download PDFInfo
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- CN1194946C CN1194946C CNB021134529A CN02113452A CN1194946C CN 1194946 C CN1194946 C CN 1194946C CN B021134529 A CNB021134529 A CN B021134529A CN 02113452 A CN02113452 A CN 02113452A CN 1194946 C CN1194946 C CN 1194946C
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Abstract
The present invention relates to a method for extracting alkene or ethene from mixed gas. At least two absorption beds operating in cycle are arranged in a variable-pressure absorption system, and the cycle operation of each absorption bed orderly comprises the following steps: absorption (A), product gas displacement (RP), vacuum pumping (V) and pressurization (ER). An absorbing agent filled in an absorbing tower is at least one of silica gel, alumina, activated carbon, carbon molecular sieves, resin, carbon adsorbing agents and zeolite molecular sieves which carry univalent copper ions Cu#+[+] and/or univalent silver ions Ag#+[+], the adsorbent temperature is from 50 to 300 DEG C, and the optimum temperature is from 80 to 150 DEG C.
Description
Technical field:
The present invention relates to from gaseous mixture to separate and the pressure swing absorption process of purified gases, particularly from contain alkene and alkane gas mixture, separate the pressure swing absorption process of purification alkene or ethene.
Technical background:
Transformation absorption be a kind of from gaseous mixture the technology of isolation of purified purifying gas, normally a kind of Gas Phase Adsorption process of carrying out at normal temperatures, pressure swing adsorption according to sorbent material different gas compositions is had the feature of adsorption selectivity and under high pressure (adsorptive pressure) loading capacity to gaseous fraction big, and in the following little characteristics of loading capacity of low pressure (desorb pressure), alternately switch circulation technology by what absorption and desorb were formed, in order to the separation of realization gas.Existing pressure swing adsorption technique all is to operate at normal temperatures, and sorbent material all has stronger adsorptive power to alkene and alkane at normal temperatures, therefore is difficult to reach the purpose of purification alkene from the mixing that contains alkene and alkane.
Summary of the invention:
Purpose of the present invention just provides a kind of pressure swing absorption process that extracts alkene or ethene from the gas mixture that contains alkene and alkane simultaneously.
The present invention uses and is loaded with univalent copper ion Cu
+And/or monovalence silver ions Ag
+Sorbent material, along with adsorption temp increases, this sorbent material weakens slower to the adsorptive power of alkene, and to other alkane, the absorption of components such as carbonic acid gas weakens comparatively fast.Under comparatively high temps, alkene more easily separates with other component.Thereby realize from gas mixture, extracting the purpose of alkene with transformation absorption.
The present invention is achieved in that
The present invention extracts alkene or the pressure swing absorption process of purification ethene from the gas mixture that contains ethene from contain olefine mixing gas, with being filled in the adsorption bed optionally adsorbs olefins and obtain alkene of sorbent material, the adsorption bed that at least two circular flows are arranged in the pressure swing adsorption system, the steps in sequence of each adsorption bed circular flow comprises absorption (A), product gas displacement (RP), vacuumize (V), (ER) step of boosting, the sorbent material that it is characterized in that loading in the adsorption tower is for being loaded with univalent copper ion Cu
+And/or monovalence silver ions Ag
+Silica gel, aluminum oxide, activated carbon, carbonaceous molecular sieve, resin, carbonaceous adsorbent, zeolite molecular sieve at least a, adsorption temp is 50～300 ℃, optimum temps is 80～150 ℃.
The present invention is extracting alkene or from the gas mixture that contains ethene in the pressure swing absorption process of purification ethene from contain olefine mixing gas, at adsorption step (A) afterwards, product gas displacement step (RP) has before along putting depressurization step (PP) or/and drop pressure step (ED).
When the present invention carries ethene in the gas mixture from contain alkene, before carrying ethylene unit, transformation absorption sets up one section transformation absorption pretreatment unit, this section apparatus occlusion and remove absorption property in the gas mixture and be better than components such as the alkene of ethene and alkane, the gaseous mixture that contains ethene after pre-treatment purifies enters back one section and carries each adsorption bed of alkene transformation absorption pretreatment unit and adsorb (A) successively, all pressure drops (ED), the reverse pressure (BD) of putting, flushing (P), all voltage rises (ER), the circulation step of (FR) finally boosts, sorbent material in the transformation absorption pretreatment unit adsorption bed is a silica gel, activated carbon, aluminium glue, activated alumina, at least a in the zeolite molecular sieve.
The temperature that the present invention extracts the displacement step in the pressure swing absorption process of alkene is 50～300 ℃, and the best is 80～150 ℃.
The present invention extracts the pressure swing absorption process of alkene, and the pressure of adsorption step is 0.1-1.9Mpa, and the pressure of said displacement step is 0.01-1.9Mpa, and the said pressure that vacuumizes step is-0.06--0.098Mpa.
The present invention extracts the displacement step in the pressure swing adsorption process of alkene, the series connection displacement that can adopt the displacement step by at least two adsorption beds to be in series and to constitute.
The pressure swing adsorption process of extraction alkene of the present invention is equipped with in each adsorption bed and is loaded with Cu
+Porous adsorbent, adsorption bed to experience absorption (A), along putting (PP) and/or all pressure drops (ED), displacement (RP), vacuumize (V), the processing steps such as (FR) that boosts adopts several combinations, alternately carry out these processing steps, so that olefin product is exported continuously.Now each step is described as follows:
Absorption (A): gas mixture enters from the adsorption bed import, and the adsorption bed pressure-controlling is at 0.05～1.9Mpa, and temperature is between 50～300 ℃, is controlled at usually between 80～150 ℃, and selected being adsorbed in of the alkene in the gas mixture is loaded with Cu
+Sorbent material on, other component is discharged from adsorption bed outlet as the absorption vent gas and is made other purposes.This step has realized separating of alkene and other component.
All pressure drops: (ED): all voltage drop step is that the adsorption bed of finishing adsorption step is put pressure to the adsorption bed of the equal voltage rise of needs, reclaims useful component and pressure in the adsorption bed, improves the process of the concentration of (alkene) in the adsorption bed.When adsorptive pressure is higher, also can arrange one suitable stride rapid (PP) before all pressing: promptly put pressure, the gas in the tower is put some come out along the adsorption gas flow direction.
Displacement (RP): return a part of olefin product to adsorption bed, adsorption bed is carried out replacement operator from bottom to top.From the displacement vent gas that adsorption bed outlet is discharged, deliver to next adsorption bed again, carry out boosting from bottom to top, all or part of returns raw material gas inlet improving the yield of alkene the gas that displacement is discharged, or discharges and make other purposes.
Vacuumize (V): the power by pump is extracted the olefin product of purifying out, carries the product gas system that goes.A part is used for displacement step.
(R) boosts: finish vacuumize step after, utilize absorption to work off one's feeling vent one's spleen, all calm the anger, one or more gases or the unstripped gas that displace implication boost to this bed.
The present invention carries ethene from the gas mixture that contains alkene, before transformation absorption purification ethylene unit, need establish one section transformation absorption pretreatment unit to remove alkene and the alkane stronger, contain propylene and the above alkene of propylene hardly thereby make in the gas mixture that enters transformation absorption purification ethylene unit than ethylene absorption ability.Transformation absorption pretreatment unit is finished a cyclical operation and will be experienced absorption (A), all pressure drops (ED), the reverse pressure (BD) of putting, flushing (P), all voltage rises (ER), the processing steps such as (FR) that finally boosts, at any time, always there are one or more adsorption beds to be in adsorption step, and under the substantially invariable situation of pressure, purified gas transferred to the adsorption bed that the ethene operation is put forward in second section transformation absorption through pipeline.Put forward the principle of transformation absorption with the transformation absorption of carrying alkene of ethene, circulation step, operational condition are the same.Below the processing step of transformation absorption pretreatment unit adsorption bed is illustrated.
Absorption (A): unstripped gas enters adsorption bed continuously and stably at 0.1～2.0Mpa pressure, and the adsorption bed pressure-controlling is at 0.05～1.9Mpa, the H in the unstripped gas
2O, propylene and molecular weight are stayed in the adsorption bed greater than the above component of propylene, and the CH that is not adsorbed
4, C
2H
4, C
2H
6, H
2Send into transformation absorption and put forward the ethene operation Deng being discharged from bed, carry out separating of ethene and other component.When adsorption bed after absorption after a while, sorbent material is saturated by macromole impurity such as propylene institutes basically, need enter single stepping for sorbent material is regenerated.
All pressure drops (ED): all to be the adsorption bed of finishing adsorption step put the process of pressure to the adsorption bed of the equal voltage rise of needs to voltage drop step, and all voltage drop step can reclaim the useful component in the adsorption bed.Equal voltage drop step can be divided into repeatedly to be finished.In concrete technological process, the equal pressure drop number of times that is adopted is looked the pressure of unstripped gas and is formed and determine.
The reverse pressure (BD) of putting: the reverse pressure of putting is that adsorption bed pressure is reduced, and makes the impurity component desorb discharging process of adsorbing in the adsorption bed.Its air flow direction is opposite with the flow of feed gas direction.
Flushing: (P): flushing is the process that the gas with the gas purging adsorption bed of component free from foreign meter boosts to this adsorption bed.All the voltage rise step can be used as repeatedly and finishes.In concrete technological process, all pressures number of times that is adopted is decided on raw gas pressure and composition.
(FR) finally boosts: this step is to utilize work in-process gas to return some to make this adsorption bed pressure be raised to the process of adsorptive pressure.
After finishing above-mentioned steps, adsorption bed has been finished the cyclical operation of one-period.The processing step of each adsorption bed experience is identical, just staggers mutually in time, thereby to guarantee an adsorption bed at any time all being arranged in the continuous operation of carrying out adsorption step operation holding device.
Pressure swing adsorption process of the present invention has following tangible advantage and significant effect.
One, uses Cu
+Porous adsorbent has stronger selectivity to alkene.
Two, strengthened the separating effect of alkene to alkane greatly being higher than under the temperature of normal temperature operation, improved the purity of product alkene, alkene purity can reach more than 98%.
Three, after the increase pre-treatment, the ethene of can purifying.
Description of drawings:
Figure one, is of the present invention a kind of from containing alkene or only containing the process flow sheet that extracts the pressure swing adsorption process of alkene or ethene the gas mixture of ethene.
Figure two, are the pressure swing adsorption technique schemas of pretreatment unit of carrying the pressure swing adsorption process of ethene from the gas mixture that contains alkene.
Figure three, are the technology time-scale of figure one.
Figure four, are the technology time-scale of figure two.
Figure five, are the technology time-scale of figure six.
Figure six, carry the pressure swing adsorption technique schema of alkene for two towers series connection metathetical is arranged.
Figure seven, are one of technology time-scale of figure.
Embodiment:
Embodiment 1:
Unstripped gas is catalysis drying gas, and is composed as follows:
Component: CH
4C
2H
4C
2H
6C
3H
8C
3H
6
Volume % (V): 37 18 18 0.4 2
Component: iso-butylene n-butene butylene carbon five
Volume % (V): 0.6 0.3 1.3 0.2
Component: H
2CO
2All the other are N for CO
2
Volume % (V): 20 1.1 0.1
The pressure swing adsorption process of present embodiment adopts the transformation shown in figure one to inhale technical process, the technology time-scale shown in the figure three according to the composition of above-mentioned raw materials.
The pressure swing adsorption system of present embodiment has adsorption bed E, F, G, the H of four tower structures, with unstripped gas pipeline G1, inlet pipe G7, displacement gas inlet pipe G12, displacement gas outlet pipe G9, pressure-equalizing passageway G10, G11, exhaust emission tube road G8, vacuum lead G13, E1 are the unstripped gas well heater, and C2 is displacement vent gas press, C3 is the displacement gas supercharger, and P1 is a vacuum pump.Each adsorption tower has 7 of sequencing valves, is respectively 1E～7E, 1F～7F, and 1G～1G, 1H～7H, the sorbent material of filling is seen figure one for being loaded with cupprous sorbent material among adsorption tower E～H, figure three.
During the pressure swing adsorption system operation, press the switch of figure three each sequencing valve of programming Control by computer.The unstripped gas of hydrocarbon-containifirst is from unstripped gas house steward G1, after entering E1 heating, press listed sequential in the pressure swing adsorption technique time-scale of table one through pipe G7, through sequencing valve 1E～1H, import from the adsorption bed bottom enters attached suction bed E, F, G, H respectively, is equipped with in each adsorption bed and is loaded with Cu
+Sorbent material, in adsorption tower, the alkene in the heated gas mixture is adsorbed by selectivity, other CH
4Discharge from the adsorption tower top through sequencing valve 2E～2H Deng component, discharge native system through pipeline G8 again and make other purposes.When adsorption bed E, F, G, H respectively after adsorption step is saturated to alkene absorption, make its pressure reduce to displacement pressure along putting and/or all pressing on gas warp in the adsorption tower, with in the olefin product partly alkene through pipeline G12, supercharger C3 is pressurized to displacement pressure as displacement gas, respectively tower E～H is replaced along the absorption direction through valve 6E～6H, displace implication and discharge adsorption tower respectively through sequencing valve 4E～4H.That discharges displaces implication through pipeline G10, G11, and sequencing valve 5E～5H enters in another adsorption tower and reclaims.The gas that exports out from another adsorption tower returns feed circuit through supercharger C2, also can go to other places to use it for anything else.Adsorption tower after the displacement is through sequencing valve 7E～7H, pipeline G13, and vacuum pump P1 extracts alkene out, obtains olefin product.
Be that example is illustrated the present embodiment technological process with the E tower below:
1, absorption (A)
Raw gas pressure 0.8Mpa is heated to 120 ℃ through E1, through sequencing valve 1E from the adsorption bed bottom inlet to the continuous charging feed gas of adsorption bed E, be adsorbed agent absorption at the adsorption bed internal olefin, discharge not adsorbed gas from tower E top through valve 2E simultaneously.When olefin(e) centent concentration reaches the setting olefin(e) centent in the discharging gas, close sequencing valve 1E, 2E, adsorption step finishes.
2, along putting (PP)
Open sequencing valve 3E, KV22, the interior gas of tower along the step-down of absorption direction, when the tower internal pressure is reduced to 0.08Mpa, close 3E, KV22.
3, all pressure drops (ED)
Open sequencing valve 4E, 5G, gas is all gone into G tower to the two pressure tower balance of just having finished evacuation step in the E tower through pipeline G10, G11.
4, displacement (RP)
Open sequencing valve 6E, 3G, KV22, displacement gas enters the E tower from 6E, along absorption direction displacement A tower, displace implication and flow out the E tower through 4E, it is higher to displace in the implication concentration of olefin, enters the G tower through G10, G11,5G and adsorbs, boosts, after the absorption, partly gas is discharged through sequencing valve 3G, through the KV23 retrieval system.Close program control 6E, 4E, 6G, 3G, KV23 after the replacement completion.
5, isolate (I)
Etc. pending next step
6, (V) finds time
Open sequencing valve 7E, product gas is through pipeline G13, and vacuum pump P1 extracts out, finds time to finish, and closes 7E.
7, isolate (I)
Etc. pending next step
8, all voltage rises (ER)
Open sequencing valve 5E, 4G, accept to boost from next all the calming the anger of G tower.
9, displacement gas boost (R)
Open 3E, KV23 and accept from what the G tower came to displace implication, absorption alkene wherein, being adsorbed partly, the gas of giving vent to anger of alkene returns feed circuit through 3E, K23.Close 3E, KV23,5E, 4G.
10, pressurization again
Open KV21,3E and utilize partly that vent gas boosts to the E tower,, close 3E, KV21 when adsorption column pressure during near adsorptive pressure.The useful raw materials gas lift that boosts is also pressed.So far, the E tower can carry out next step round-robin adsorption process again.
The circulation step of other three towers is the same with the E tower, just staggers mutually on the time.See figure one, figure three.
This embodiment can obtain 95-99% (V) olefin product purity, and product recovery rate is greater than 80%.
Embodiment 2:
The present embodiment unstripped gas is identical with embodiment 1, and extracting product is pure ethylene.
Present embodiment adopts two sections transformations absorption serial operations, and first section be pretreatment unit, and its effect is to remove propylene and molecular weight greater than the alkene more than the propylene, and the while is also removed propylene and the above alkane of propane.The ethene mixed gas that contains of having removed propylene, propane and above hydro carbons enters second section transformation absorption, purification ethene.
The transformation absorption pretreatment unit process flow sheet of present embodiment is figure two, extracts the pressure-swing absorption apparatus process flow sheet one of ethene.The ethene gas mixture that contains that pretreatment unit removes components such as propylene enters through outlet pipe G2 and carries the ethene pressure-swing absorption apparatus, and it is identical with embodiment one with service temperature to carry the ethylene unit processing step.We stress the technological process of refining plant at this, see figure two, figure four.
As figure two, in refining plant, adsorption bed A, B, C, the D of four tower structures arranged, unstripped gas inlet pipe G1, waste gas blow-down pipe G5, work in-process tracheae G2, all pressure and forcing pipe G3 again, purge tracheae G4.Each adsorption tower has 5 of sequencing valves, is respectively 1A～5A, 1B～5B, and 1C～5C, 1D～5D, pressurizing valve is KV1 again.
The sorbent material of filling is the combination cot of aluminum oxide and activated carbon among adsorption tower A～D, and aluminum oxide is following, and activated carbon is last.Adsorption temp≤40 ℃.
During the operation of transformation absorption pretreatment unit, press the switch of figure four each sequencing valve of programming Control by computer, unstripped gas is pressed sequential in the table four pressure swing adsorption technique time-scale through house steward G1, enter adsorption bed A, B, C, D from the import of adsorption bed bottom respectively through sequencing valve 1A～1D, in adsorption tower, propylene reaches with the selected absorption of first-class component, and other component such as ethene is discharged from the adsorption tower top through sequencing valve 2A～2D, is referred to as work in-process gas.This part gas enters transformation absorption and carries olefin hydrocarbon apparatus after pipeline G2 goes well heater E1 heating, the operating procedure of carrying olefin hydrocarbon apparatus is identical with embodiment 1 with operational condition, at this purification ethene, when adsorption bed A, B, C, D respectively when the absorb leading-edge of adsorption step propylene arrives certain position in the adsorption bed, stop absorption, the gas in the adsorption bed and other bed are all pressed.
Contrary then putting to normal pressure utilized from the outlet vent gas of carrying the ethene pressure-swing absorption apparatus the reverse purging of pretreatment unit adsorption bed, makes bed obtain regeneration, accepts all to calm the anger then to boost, and finally is depressed into adsorptive pressure with the work in-process gas lift.
Now be, transformation absorption pretreatment unit is illustrated, see figure two, figure four with the A tower.
1, absorption (A): raw gas pressure 0.8Mpa, 40 ℃ of temperature, through sequencing valve 1E from the adsorption bed bottom inlet to the continuous charging feed gas of adsorption bed A, be adsorbed agent absorption at components such as adsorption bed inner propenes, discharge work in-process gas from tower A top through valve 2A simultaneously, when the absorb leading-edge of propylene in the adsorption bed reaches certain position, close sequencing valve 1A, 2E, adsorption step finishes.
2, one all falls (E1D)
Open sequencing valve 3A, 3C, the gas of A tower enters the C tower, closes 3C after the two pressure tower equilibriums.
3, two all fall (E2D)
Open sequencing valve 3D, the gas of A tower enters the D tower, after the two pressure tower equilibriums, closes 3D.
4, contrary put (BD)
Open sequencing valve 5A, allow in the A tower gas against the emptying of absorption direction, when pressure near normal pressure, this moment, sorbent material was necessarily regenerated.
5, purge (PP)
Open sequencing valve 4A, utilize the reverse purging of the vent gas A tower of carrying ethylene unit, purge when finishing, absorption obtains regeneration.Close 4A, 5A.
6, two all rise (E2R)
Open sequencing valve 3D, 3A, accept to boost, after the two pressure tower equilibriums, close 3D, 3A from the gas that the D tower comes.
7, isolate (I)
Etc. pending next step
8, one all rise (E1R)
Open program control 3C, 3A, accept to boost, after the two pressure tower equilibriums, close 3C, 3A from next all the calming the anger of C tower.
9, isolate (I)
Etc. pending next step
10, pressurization (FR) again
Open KV1,3A, with work in-process gas to the A tower until near adsorptive pressure, close KV1,3A.
So far, the A tower has been finished a circulation, can carry out next round-robin adsorption step again, and the operating procedure of other three towers is the same with the A tower, just staggers mutually on the time.
Through two sections transformation absorption, can be from containing the transformation adsorbing and extracting ethene of multiple alkene, present embodiment can extract the ethene that concentration is 90～98% (V), and yield of ethene is greater than 80%.
Embodiment 3:
The present embodiment unstripped gas is identical with embodiment 1, adopts to have the be in series technology of the series connection displacement step that constitutes of two adsorption bed displacement step and extract alkene.The present embodiment technical process is shown in figure six, and the technology sequential is shown in figure five.Filling is loaded with Cu among adsorption tower I～L
+Sorbent material.Be example explanation present embodiment now with the I tower.
1, absorption (A)
Material pressure 0.1～0.2Mpa, enter well heater E2 through V4 and be heated to 130 ℃, enter adsorption tower I through pipeline G19, sequencing valve 1I, be attracted on the sorbent material at the adsorption tower internal olefin, discharge not adsorbed gas from the adsorption bed top through sequencing valve 2I simultaneously, when the absorb leading-edge of alkene arrives in the tower certain position, close 1I, 2I.
2, all pressure drops (ED)
Open sequencing valve 6I, gas in the adsorption bed I all is pressed into the J tower, the J tower is boosted, close 6I after the two tower balances.
3, displace implication displacement (RP2)
Open sequencing valve 6L, with displacing implication introducing I tower the second time in the L tower I tower is carried out replacing the first time I bed, open sequencing valve 3I, KV32, displace implication through pipeline G18, compressor C2 returns raw material tracheae G15.Close 6L, 3I, KV32.
4, displacement (RP1) for the second time
Open sequencing valve 4I, 6I, the portioned product alkene that supercharger G5 is provided is used for replacing for the second time the I bed.Concentration of olefin is higher from the gas that the I top of tower comes out, and is used for the displacement first time of J bed.Close 4I, 6I.
5, (V1, V2) finds time
Open sequencing valve 5I, product alkene is through pipeline G21, and vacuum pump P2 extracts out, and G24 goes down operation through pipeline.Close 5I.
6, (ER) boosts
Open sequencing valve 6L, make the gas of the L tower that is in equal voltage drop step enter the I tower, the I tower is boosted, close 6L.
So far the I tower has been finished a circulation, can carry out adsorption step again, and at the adsorption step initial stage, unstripped gas also will continue the I tower is boosted.The step of other three tower is identical with the I tower, just staggers mutually on the time.See figure five.
The alkene purity that present embodiment obtains is greater than 95%, and yield is greater than 80%.
Embodiment 4:
The unstripped gas of present embodiment is polypropylene tail gas, and is composed as follows:
Component C H
4C
2H
4C
2H
6C
3H
8C
3H
6
Concentration V% 21.7 0.26 9.3 68.7
The pressure swing adsorption process of present embodiment adopts the pressure swing adsorption technique flow process shown in the figure one according to the composition of above-mentioned raw materials gas, the technology time-scale shown in the figure seven, and filling is loaded with Cu among adsorption tower E～H
+With Ag
+Sorbent material.
Be example explanation present embodiment now with the E tower.
1, absorption (A)
Raw gas pressure 0.05Mpa, through pipeline G1, valve V3 enters well heater E1 and is heated to 150 ℃, opens sequencing valve 1E, 2E, unstripped gas is through pipeline G7, and G14 enters the E tower, and alkene is adsorbed agent absorption in the E tower, the gas that is not adsorbed is through 2E, and pipeline G8 discharges, and closes 1E, 2E.
2, displacement (RP)
Open sequencing valve 6E, 4E, 5G, through the part product gas of supercharger C3 supercharging, 100～150 ℃ of temperature enter the E tower through pipeline G12 the E tower are replaced, and metathetical is worked off one's feeling vent one's spleen and entered the G tower through pipeline G10, G11 the G tower is boosted.Close 6E, 4E, 5G.
3, (V) finds time
Open sequencing valve 7E, product alkene is extracted out through pipeline G13, vacuum pump P1 in the tower, and G15 goes down operation through pipeline.Close 7E.
4, (R) boosts
Open sequencing valve 5E, accept the E tower to be boosted, close 5E from the implication that displaces that the G tower comes.
5, the FR that finally boosts
Open sequencing valve KV21,3E, utilizing partly, vent gas boosts to the E tower.Close KV21,3E.
So far, the E tower is finished a circulation, can carry out absorption next time again, and the step of other three towers is identical with the E tower, just staggers on the time.
V2 among Fig. 1, V3 are valve, and G14 is a pipeline, the G10 among Fig. 6, and G17, G20, G25, G22I, G23I, G23J, J23K, J23L is pipeline.The G1 of Fig. 1 is the unstripped gas pipeline, and the G2 among Fig. 2 is the work in-process feed channel.
Present embodiment alkene purity is greater than 95%.Yield is greater than 85%.
Claims (8)
1, a kind of method of from gas mixture, extracting alkene or ethene, in pressure swing adsorption system, the adsorption bed that has two circular flows at least, the steps in sequence of each adsorption bed circular flow comprises absorption (A), product gas displacement (RP), vacuumize (V), (ER) step of boosting, the sorbent material that it is characterized in that loading in the adsorption tower is for being loaded with univalent copper ion Cu
+And/or monovalence silver ions Ag
+Silica gel, aluminum oxide, activated carbon, carbonaceous molecular sieve, resin, carbonaceous adsorbent, zeolite molecular sieve at least a, adsorption temp is 50～300 ℃.
2, according to the described pressure swing absorption process of claim 1, it is characterized in that adsorption step (A) afterwards, product gas displacement step (RP) has before along putting depressurization step (PP) or/and drop pressure step (ED).
3, according to claim 1 or 2 described pressure swing absorption process, when it is characterized in that in the gas mixture from contain multiple alkene purification ethene, before carrying ethylene unit, transformation absorption sets up one section transformation absorption pretreatment unit, this section apparatus occlusion and remove absorption property in the gas mixture and be better than components such as the alkene of ethene and alkane, the gaseous mixture that contains ethene after pre-treatment purifies enters back one section and carries each adsorption bed of alkene transformation absorption pretreatment unit and adsorb (A) successively, all pressure drops (ED), the reverse pressure (BD) of putting, flushing (P), all voltage rises (ER), the circulation step of (FR) finally boosts, sorbent material in the transformation absorption pretreatment unit adsorption bed is a silica gel, activated carbon, aluminium glue, activated alumina, at least a in the zeolite molecular sieve.
4, according to the described pressure swing absorption process of claim 1, the temperature that it is characterized in that product gas displacement step (RP) is 50～300 ℃.
5, according to claim 1 or 2 described pressure swing absorption process, the pressure that it is characterized in that adsorption step is 0.1-1.9Mpa, and the pressure of said displacement step is 0.01-1.9Mpa, and the said pressure that vacuumizes step is-0.06--0.098Mpa.
6, according to claim 1 or 2 described pressure swing absorption process, the series connection displacement that it is characterized in that having the displacement step by at least two adsorption beds to be in series and to constitute.
7,, it is characterized in that adsorption temp is 80～150 ℃ according to the described pressure swing absorption process of claim 1.
8, according to the described pressure swing absorption process of claim 1, the temperature that it is characterized in that product displacement step (RP) is 80～150 ℃.
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| CN102329642B (en) * | 2011-06-22 | 2015-08-19 | 中国石油化工股份有限公司 | Remove the method for propylene and more than C3 component in catalytic cracked dry gas |
| CN103304358B (en) * | 2013-05-29 | 2015-06-03 | 中建安装工程有限公司 | Separating method and equipment of low-carbon olefins beneficial to product recovery |
| CN108469471A (en) * | 2017-02-23 | 2018-08-31 | 中国石油化工股份有限公司 | The solid-phase extraction column and application process of different Group Components in separating synthetic gas olefine reaction oil-phase product |
| JP7023736B2 (en) * | 2018-02-16 | 2022-02-22 | 大陽日酸株式会社 | Gas purification equipment, gas purification method, propene production equipment and propane production equipment |
| CN113041782B (en) * | 2021-03-15 | 2021-12-17 | 西南化工研究设计院有限公司 | Gas pressure swing adsorption separation and purification system and separation and purification method thereof |
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