CN102935324B - Variable pressure absorption method for increasing absorption phase product yield - Google Patents
Variable pressure absorption method for increasing absorption phase product yield Download PDFInfo
- Publication number
- CN102935324B CN102935324B CN201210394237.3A CN201210394237A CN102935324B CN 102935324 B CN102935324 B CN 102935324B CN 201210394237 A CN201210394237 A CN 201210394237A CN 102935324 B CN102935324 B CN 102935324B
- Authority
- CN
- China
- Prior art keywords
- pressure
- adsorption
- variable
- sections
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Abstract
The present invention discloses a variable pressure absorption method for increasing absorption phase product yield, wherein a variable pressure absorption system comprises a variable pressure absorption segment 1, a variable pressure absorption segment 2 and a variable pressure absorption segment 3, every variable pressure absorption segment respectively comprises at least two absorption towers filled with an absorption agent, every absorption tower of the variable pressure absorption segment 1 and the variable pressure absorption segment 2 is at least sequentially and circularly subjected to steps of absorption, displacement, evacuation and pressure increasing, displaced waste gas from the variable pressure absorption segment 1 and the variable pressure absorption segment 2 is adopted as raw material gas and enters the variable pressure absorption segment 2, every absorption tower of the variable pressure absorption segment 3 is at least sequentially and circularly subjected to steps of absorption, reverse releasing or evacuation, and pressure increasing, absorbed waste gas from the variable pressure absorption segment 1 and the variable pressure absorption segment 2 is adopted as raw material gas of the variable pressure absorption segment 3 and enters the variable pressure absorption segment 3, and reverse releasing gas or evacuation gas of the variable pressure absorption segment 3 returns to the variable pressure absorption segment 1, and is adopted as raw material gas of the variable pressure absorption segment 1.
Description
Technical field
The present invention relates to a kind of from gaseous mixture separated pressure-variable adsorption (PSA) method that reclaims Adsorption Phase product, particularly relate to and a kind ofly in separation, reclaim the pressure swing absorption process that includes displacement step in Adsorption Phase product process.
Background technology
Pressure swing absorption process be utilize porosu solid adsorbent under certain pressure to mist in the different component characteristic with selective absorption realize the separation of mist.As required separated product in adsorbent bed in absorption or non-adsorbed state can be divided into Adsorption Phase product and fluid phase product.The existing separated carbon dioxide reclaiming in synthetic-ammonia transformation gas, the separated carbon monoxide that reclaims in water-gas, semiwater gas from carbon dioxide removal, and the separated hydrocarbon component reclaiming in mist, as separating and reclaiming ethylene, ethane and C from oil plant catalytic cracked dry gas
2in the pressure swing adsorption of the Adsorption Phase products such as above component, in order to improve the content of Adsorption Phase product, adopted the technique of returning part gas product displacement sorption bed.Replacing process has improved the purity of Adsorption Phase product, also make the dividing potential drop of absorber port of export Adsorption Phase product improve simultaneously, impact due to find time efficiency and Adsorption Phase product desorption resistance to mass tranfer on adsorbent of vavuum pump, in the decompression desorption stage of pressure-variable adsorption separation process, absorber outlet section can nubbin be failed the Adsorption Phase product of complete desorption, this portioned product can be adsorbed waste gas and take absorber out of in ensuing adsorption process, cause the reduction of Adsorption Phase product recovery rate, affect the economic benefit of pressure-swing absorption apparatus.The patent ZL200510129369.3 of Sichuan Tianyi Science & Technology Co., Ltd and patent ZL200510118241.7 disclose the method that adopts two-phase method pressure-variable adsorption to reclaim Adsorption Phase product in displacement waste gas, solve displacement waste gas and reduced the problem of Adsorption Phase product recovery rate, but failed to relate to the problem of taking Adsorption Phase product out of in absorption waste gas and reducing Adsorption Phase product recovery rate that solves.
Summary of the invention
For above-mentioned the deficiencies in the prior art, the object of the present invention is to provide a kind of from gaseous mixture the pressure swing absorption process of separated Adsorption Phase product, the method can improve the rate of recovery of product in including the pressure-swing absorption process of displacement step.
Above-mentioned purpose of the present invention is achieved by the following technical solution:
A kind of pressure swing absorption process that improves Adsorption Phase product recovery rate, it is characterized in that, this pressure swing adsorption system comprises 3 sections of 1 section of pressure-variable adsorption and 2 sections of pressure-variable adsorptions and pressure-variable adsorptions, every section of pressure-variable adsorption consists of at least two adsorption towers that are filled with adsorbent respectively, each adsorption tower that 1 section of pressure-variable adsorption and pressure-variable adsorption are 2 sections circulates at least successively and experiences absorption, displacement, find time, the step of boosting, and the displacement waste gas that pressure-variable adsorption is 1 section enters 2 sections of pressure-variable adsorptions as unstripped gas, each adsorption tower that pressure-variable adsorption is 3 sections circulates at least successively and experiences absorption, inverse put, the step of boosting, or the absorption of circulation experience at least successively, find time, the step of boosting, the absorption waste gas that pressure-variable adsorption is 1 section is as the unstripped gas of 3 sections of pressure-variable adsorptions, enter 3 sections of pressure-variable adsorptions, after the inverse put gas that pressure-variable adsorption is 3 sections and exhaust supercharging, mix with the unstripped gas of 1 section of pressure-variable adsorption as unstripped gas and introduce 1 section of pressure-variable adsorption.
As preferably, the unstripped gas that pressure-variable adsorption is 2 sections can also comprise the displacement waste gas of 2 sections of pressure-variable adsorptions.
In addition, the unstripped gas of 3 sections of pressure-variable adsorptions can also comprise the absorption waste gas of 2 sections of pressure-variable adsorptions.
Further, in the present invention, according to raw gas pressure and displacement gas pressure, increase the one or more of the following step, after the adsorption step of 2 sections of 1 section of pressure-variable adsorption and pressure-variable adsorptions, increase by 1 time or equal voltage drop step repeatedly, after displacement step, increase by 1 time or equal voltage drop step repeatedly, before evacuation step, increase inverse put step, after evacuation step, increase the equal voltage rise step of one or many, in 3 sections of absorption of circulation experience successively of pressure-variable adsorption, inverse put, find time, the step of boosting, and after adsorption step, increase by 1 time or equal voltage drop step repeatedly, before the step of boosting, increase the equal voltage rise step of one or many, the inverse put gas that pressure-variable adsorption is 3 sections and exhaust return to 1 section of unstripped gas as 1 section of pressure-variable adsorption of pressure-variable adsorption.
Example of the present invention is as follows: adopt three sections of interconnective pressure-swing absorption apparatus, at 1 section of pressure-variable adsorption and 2 sections of each adsorption towers of pressure-variable adsorption, circulate at least successively experience absorption, displacement, inverse put, find time, five steps finally boosts.According to parameters such as the pressure of concrete technology, purity, between absorption and inverse put step, also can comprise at least one times or equal voltage drop step repeatedly, all voltage drop step, immediately after adsorption step, also can be carried out after displacement step; And immediately at least one times or repeatedly all voltage rises after evacuation step.
In pressure-swing absorption process, the 1st stage pressure swing adsorption apparatus is processed the Adsorption Phase product in the unstripped gas that enters pressure swing adsorption system, from inverse put gas and exhaust, obtain the gas product of Adsorption Phase component, directly returning part gas product or returning part gas product have entered adsorption step or have had the adsorption tower equal voltage drop step from adsorption tower unstripped gas arrival end after pressurization, the impurity of a small amount of fluid phase product of adsorbing in displacement sorption tower space and on adsorbent, to improve the concentration of Adsorption Phase product component in adsorption tower.
The gas of emitting from the adsorption tower port of export in the displacement step of pressure-variable adsorption is called displacement waste gas.In the present invention, more preferably the displacement waste gas of 2 sections of 1 section of pressure-variable adsorption and pressure-variable adsorptions enters 2 sections of pressure-variable adsorptions as unstripped gas, by absorption again, further reclaims in displacement waste gas easily the product gas of absorption to reach the object that improves the gas product rate of recovery.
1 section of pressure-variable adsorption is introduced to 3 sections of pressure-variable adsorptions with the absorption waste gas of 2 sections of pressure-variable adsorptions, by the adsorbent loading in 3 sections of absorbers of pressure-variable adsorption, Adsorption Phase product component in 1 section of pressure-variable adsorption of absorption absorption waste gas, be rich in Adsorption Phase product 3 sections of pressure-variable adsorptions inverse put gas or and exhaust after pressurization, return to 1 section of pressure-variable adsorption and mix unstripped gas as 1 section of pressure-variable adsorption with the unstripped gas of 1 section of pressure-variable adsorption through pressure-swing absorption apparatus recovery Adsorption Phase product.Circulate at least successively experience absorption, inverse put or the step of finding time, boost of each adsorption tower in 3 sections of pressure-variable adsorptions, as preferably, according to parameters such as the pressure of concrete technology, purity, between absorption and inverse put step, also can comprise at least one times or equal voltage drop step repeatedly, and evacuation step after immediately at least one times or repeatedly equal voltage rise.
In the present invention, " a plurality of " in term " one or more " are at least two, are preferably three; " repeatedly " in " one or many " is at least twice, is preferably three times.
The adsorbent of selecting in adsorption step of the present invention is at least one in active carbon, activated alumina, silica gel and molecular sieve.The selection of adsorbent and be used in combination can be according to the composition of processed gaseous mixture or changes of contents and determine.
In above-mentioned pressure swing absorption process, the adsorption step pressure of 1 section of pressure-variable adsorption is greater than 0.15MPa; the adsorption step pressure that pressure-variable adsorption is 2 sections is the displacement exhaust gas pressure of 1 section of pressure-variable adsorption; displacement step pressure is greater than 0.1Mpa; the adsorptive pressure that pressure-variable adsorption is 3 sections is that the pressure of 1 section of absorption waste gas of pressure-variable adsorption can be greater than 0.12MPa conventionally; inverse put step pressure is greater than 0.1Mpa, and evacuation step pressure is 0.01～0.07MPa.(pressure all represents by absolute pressure)
Pressure swing absorption process of the present invention is applicable to obtain from Adsorption Phase the pressure swing adsorption system of product, for example from synthetic-ammonia transformation gas, carbon dioxide is reclaimed in separation, the separated carbon monoxide that reclaims in water-gas from carbon dioxide removal, semiwater gas, and the separated hydrocarbon component reclaiming in mist, as separating and reclaiming ethylene, ethane and C from oil plant catalytic cracked dry gas
3above component etc.
In above-mentioned pressure swing adsorption technique of the present invention, 2 sections of 1 section of pressure-variable adsorption and pressure-variable adsorptions will experience absorption, displacement, inverse put, the step of finding time, boost in the once circulation of each adsorption tower, in the once circulation of 3 sections of each adsorption towers of pressure-variable adsorption, to experience absorption, all pressure drop, inverse put, find time, all voltage rise with boost step and according to adsorptive pressure, absorption exhaust gas concentration require, the process conditions such as separated recovery Adsorption Phase product purity requirement, can reasonably accept or reject equal pressure drop, equal voltage rise step, arrangement and number of times setting.Each adsorption tower in every section of absorbing unit is by the identical step of experience, and each tower just staggers in time mutually, so that device is continuous, stable operation.
Can be as follows for each step detailed process adopting in 2 sections of 1 section of the above-mentioned pressure-variable adsorption of the present invention and pressure-variable adsorptions:
Absorption A
Containing the mist easily adsorbing and be difficult for absorbed component, from adsorption tower import, enter adsorbent bed, adsorption column pressure is greater than 0.05Mpa, 5～60 ℃ of temperature, easy absorbed component in mist is adsorbed the adsorbent absorption of loading in tower, and the component that is difficult for absorption is discharged and is called as absorption waste gas from adsorption tower outlet.This step realizes easy absorbed component and is difficult for the separated of absorbed component.
Equal pressure drop ED
All voltage drop step is adsorption step to be completed or adsorption tower that displacement step completes, by pipeline and sequencing valve, be communicated with the adsorption tower that enters equal voltage rise step, reclaim useful constituent and pressure in equal voltage drop step adsorption tower, improve the content of Adsorption Phase component in adsorption tower.All voltage drop step can be arranged to 1 time according to adsorptive pressure, or repeatedly as one all fall E1D and two and all fall E2D.
Displacement RP
The Adsorption Phase gas product of returning part inverse put and the acquisition of finding time, to completing the adsorption tower of adsorption step, from raw material gas inlet end, enter adsorbent bed, utilize gas product that Adsorption Phase constituent content is higher to the impurity in adsorbent bed adsorbent space, replace with a small amount of impurity adsorbing in adsorbent, improve the content of Adsorption Phase component in adsorption tower.The displacement waste gas that displacement step is discharged from adsorption tower outlet in the present invention enters the unstripped gas that 2 sections of pressure-variable adsorptions are used as 2 sections of pressure-variable adsorptions.
Inverse put D
Displacement step is completed or displacement step has been carried out again the adsorption tower of equal voltage drop step after completing, open the sequencing valve that connects adsorption tower unstripped gas arrival end, discharge the gas in adsorption tower, reduce the pressure of adsorption tower, make to be adsorbed on the Adsorption Phase component partial solution sucking-off adsorbent in adsorption tower, obtain Adsorption Phase product.
V finds time
Adsorption tower after utilizing vavuum pump to inverse put is found time, and further reduces the pressure of adsorption tower, and the Adsorption Phase product that makes to be adsorbed in adsorbent is further separated sucking-off adsorbent, obtains Adsorption Phase product.
Equal voltage rise ER
Adsorption tower after evacuation step is completed, by pipeline, be connected with the adsorption tower in equal voltage drop step with sequencing valve, make the gas in equal voltage drop step adsorption tower that pressure is higher enter the adsorption tower of equal voltage rise, with the pressure of the equal voltage rise adsorption tower that raises, and the Adsorption Phase product in the equal pressure drop gas of recovery section.All voltage rise step can be arranged to 1 time according to adsorptive pressure, or repeatedly as two all rise E2R and and all rise E1R.
(FR) boosts
Utilize the adsorption tower after absorption waste gas completes equal voltage rise step to boost, make it to reach adsorptive pressure, prepare to enter adsorption step.
Can be as follows for each step detailed process adopting in 3 sections of above-mentioned pressure-variable adsorptions of the present invention:
Absorption A
Containing the mist easily adsorbing and be difficult for absorbed component, from adsorption tower import, enter adsorbent bed, adsorption column pressure is greater than 0.05Mpa, 5～60 ℃ of temperature, easy absorbed component in mist is adsorbed the adsorbent absorption of loading in tower, and the component that is difficult for absorption is discharged and is called as absorption waste gas from adsorption tower outlet.This step realizes easy absorbed component and is difficult for the separated of absorbed component.
Equal pressure drop ED
All voltage drop step is the adsorption tower that adsorption step is completed, and by pipeline and sequencing valve, is communicated with the adsorption tower that enters equal voltage rise step, reclaims useful constituent and pressure in equal voltage drop step adsorption tower, improves the content of Adsorption Phase component in adsorption tower.All voltage drop step can be arranged to 1 time according to adsorptive pressure, or repeatedly as one all fall E1D and two and all fall E2D.
Inverse put D
Displacement step is completed or displacement step has been carried out again the adsorption tower of equal voltage drop step after completing, open the sequencing valve that connects adsorption tower unstripped gas arrival end, discharge the gas in adsorption tower, reduce the pressure of adsorption tower, make to be adsorbed on the Adsorption Phase component partial solution sucking-off adsorbent in adsorption tower, obtain Adsorption Phase product.
V finds time
Adsorption tower after utilizing vavuum pump to inverse put is found time, and further reduces the pressure of adsorption tower, and the Adsorption Phase product that makes to be adsorbed in adsorbent is further separated sucking-off adsorbent, obtains Adsorption Phase product.
Equal voltage rise ER
Adsorption tower after evacuation step is completed, by pipeline, be connected with the adsorption tower in equal voltage drop step with sequencing valve, make the gas in equal voltage drop step adsorption tower that pressure is higher enter the adsorption tower of equal voltage rise, with the pressure of the equal voltage rise adsorption tower that raises, and the Adsorption Phase product in the equal pressure drop gas of recovery section.All voltage rise step can be arranged to 1 time according to adsorptive pressure, or repeatedly as two all rise E2R and and all rise E1R.
(FR) boosts
Utilize the adsorption tower after absorption waste gas completes equal voltage rise step to boost, make it to reach adsorptive pressure, prepare to enter adsorption step.
Beneficial effect of the present invention is: improve Adsorption Phase product recovery rate 5%～10%.
Accompanying drawing explanation
Fig. 1 is the process chart of the preferred embodiment of the present invention.
Below the present invention is further detailed explanation for the embodiment by the specific embodiment.But this should be interpreted as to the scope of the above-mentioned theme of the present invention only limits to following embodiment.Without departing from the idea case in the present invention described above, various replacements or the change according to ordinary skill knowledge and customary means, made, include within the scope of the invention.
the specific embodiment
Embodiment 1
The present embodiment is the pressure swing adsorption method of separating and reclaiming ethylene from oil plant catalytic cracked dry gas, dry gas flow 30000Nm
3/ h, its gas componant forms as shown in table 1:
Table 1 dry gas becomes to be grouped into V%
。
The present embodiment pressure swing adsorption system is formed with 3 sections of PSA-3 of pressure-variable adsorption and is formed by 1 section of PSA-1 of pressure-variable adsorption, 2 sections of PSA-2 of pressure-variable adsorption.Unstripped gas enters 1 section of pressure-variable adsorption, the displacement waste gas that pressure-variable adsorption is 1 section enters 2 sections of unstripped gas as 2 sections of pressure-variable adsorptions of pressure-variable adsorption, from 1 section of pressure-variable adsorption, obtain ethylene-rich product and displacement gas with inverse put gas and the exhaust of 2 sections of pressure-variable adsorptions, the absorption waste gas that 1 section of pressure-variable adsorption and pressure-variable adsorption are 2 sections enters 3 sections of unstripped gas as 3 sections of pressure-variable adsorptions of pressure-variable adsorption, after the inverse put that pressure-variable adsorption is 3 sections and exhaust supercharging, returning to 1 section of pressure-variable adsorption mixes with unstripped gas as pressure-variable adsorption unstripped gas, the absorption waste gas output device that pressure-variable adsorption is 3 sections goes recover hydrogen or as fuel gas.
PSA-1 is formed by connecting by 10 adsorption towers and corresponding pipeline.Circulate each time all experience absorption A, displacement RP, of every tower all falls E1D, two and all falls E2D, the reverse D of bleeding off pressure, the V that finds time, two and all rise E2R, and all rise E1R, final nine steps of FR of boosting, and its program operation sequential is in Table 2.
Table 2 PSA-1 work schedule table
。
The adsorption tower A in PSA-1 of now take shown in Fig. 1 is example, each processing step of narration PSA-1 operation:
Absorption A
Catalytic cracked dry gas enters adsorption tower A, C as unstripped gas
2h
4etc. easy absorbed component, be attracted on adsorbent, absorption waste gas goes out-of-bounds.
Displacement RP
Gas from displacement gas compressor is replaced adsorption tower A by adsorption tower from bottom to top via oil expeller, displacement gas surge tank, control valve, and the impurity component in tower is out replaced, and displacement waste gas is the unstripped gas as PSA-2 to displacement off-gas buffer tank.
One all falls E1D
Gas in adsorption tower A and adsorption tower T101G carry out isostasy, and when two pressure towers equate substantially, this step finishes.
Two all fall E2D
Gas in adsorption tower A and adsorption tower T101H carry out isostasy, and when two pressure towers equate substantially, this step finishes.
Inverse put D
Elevated pressures portion gas in adsorption tower A, reverse bleeding off pressure enters one section of inverse put gas surge tank, when adsorption tower A and surge tank approach balance, the lower gas of inverse put pressure is with the gas in one section of inverse put gas surge tank through step-down, send into together half gas product surge tank and carry out reverse bleeding off pressure, when adsorption tower A and half gas product surge tank approach balance, this step finishes.
V finds time
Vavuum pump directly vacuumizes adsorption tower A, and half product gas that vavuum pump is extracted out is chilled to after 40 ℃ and goes to mix with half gas product surge tank inverse put gas phase out through cooler.Pressure process is by drop to-0.08MPa of 0.02MPa.
Two all rise E2R
In adsorption tower D, gas enters adsorption tower A, carries out isostasy, and when two pressure towers equate substantially, this step finishes.
One all rises E1R
In adsorption tower E, gas flows into adsorption tower A, carries out isostasy, and when two pressure towers equate substantially, this step finishes.
FR finally boosts
Absorption waste gas enters adsorption tower A and finally boosts.When adsorption tower A pressure approaches adsorptive pressure substantially, this step finishes.
So far, the institute of adsorption tower A in one-period is all finished in steps, and starts to enter next time circulation, and the performed step of other nine adsorption towers is identical with adsorption tower A, just mutually staggers in time, to guarantee that separation process carries out continuously.
Each adsorption column pressure is cyclically-varying with the variation of processing step, and according to practical operation situation, adsorptive pressure can suitably be adjusted, other step pressure is corresponding changes.
PSA-2 is formed by connecting by six adsorption towers and corresponding pipeline.Each cyclic process experience absorption A, displacement RP, all pressure drop ED, inverse put D, the V that finds time, all voltage rise ER, final seven steps of FR of boosting, its each tower operation sequential in Table 3 in Table.
Table 3 PSA-2 work schedule table
。
Now take adsorption tower A as example, each processing step of narration PSA-2 operation:
Absorption A
From the displacement waste gas of PSA-1, through displacement off-gas buffer tank, as the unstripped gas of PSA-2, enter adsorption tower A, C in unstripped gas
2 +component is stayed in adsorbent bed by preferential absorption, weak adsorbent component H
2, N
2absorption waste gas Deng impurity with PSA-1 goes out-of-bounds.
Displacement RP
Half product gas from displacement gas compressor is replaced adsorption tower A by adsorption tower from bottom to top, impurity component in tower is out replaced, displacement waste gas goes out-of-bounds with the absorption waste gas of PSA-1, or after mixing with the displacement waste gas of PSA-1, as unstripped gas, enters 2 sections of pressure-variable adsorptions and adsorb.
Equal pressure drop ED
Gas in adsorption tower A and adsorption tower D carry out isostasy, and when two pressure towers equate substantially, this step finishes.
Inverse put D
In adsorption tower A, gas carries out reverse bleeding off pressure against the direction of absorption, against being deflated to two sections of inverse put tanks, again to half gas product surge tank, when adsorption tower internal pressure and inverse put pressure tank equate substantially, in adsorption tower, the direct inverse put of gas is to half gas product surge tank, adsorption tower internal pressure is down to while equating with half gas product surge tank pressure, and this step finishes.
V finds time
Vavuum pump directly vacuumizes adsorption tower A, and half product gas that vavuum pump is extracted out enters half gas product surge tank after cooler is chilled to 40 ℃ to be mixed with inverse put gas phase.Pressure process is by drop to-0.08MPa of 0.02MPa.
Equal voltage rise ER
In adsorption tower D, gas flows into adsorption tower A, carries out isostasy, and when two pressure towers equate substantially, this step finishes.
FR finally boosts
Absorption waste gas enters adsorption tower A and finally boosts.When adsorption tower A pressure approaches adsorptive pressure substantially, this step finishes.
So far, all seven steps of adsorption tower A in one-period are all finished, and start to enter next time circulation, and the performed step of other four adsorption towers is identical with adsorption tower A, just mutually stagger in time, to guarantee that separation process carries out continuously.
Each adsorption column pressure is cyclically-varying with the variation of processing step, and according to practical operation situation, adsorptive pressure can suitably be adjusted, other step pressure is corresponding changes.
PSA-3 is formed by connecting by eight adsorption towers and corresponding pipeline.Each cyclic process experience absorption A, all falls that ED2, inverse put D all fall in ED1, two, the V that finds time, two all rises ER2, and all rises ER1, final eight steps of FR of boosting, its each tower operation sequential in Table 4 in Table.
Table 4 PSA-3 work schedule table
。
Now take adsorption tower A as example, each processing step of narration PSA-3 operation:
Absorption A
From the absorption waste gas of PSA-1 and PSA-2, as the unstripped gas of PSA-3, enter adsorption tower A, wherein C
2 +component is stayed in adsorbent bed by preferential absorption, containing weak adsorbent component H
2, N
2absorption waste gas output device Deng impurity.
One equal pressure drop E1D
Gas in adsorption tower A and adsorption tower E carry out isostasy, and when two pressure towers equate substantially, this step finishes.
Two equal pressure drop E2D
Gas in adsorption tower A and adsorption tower F carry out isostasy, and when two pressure towers equate substantially, this step finishes.
Inverse put D
In adsorption tower A, gas carries out reverse bleeding off pressure against the direction of absorption, against being deflated to three sections of inverse put gas surge tanks.
V finds time
Vavuum pump directly vacuumizes adsorption tower A, and half product gas that vavuum pump is extracted out enters half gas product surge tank after cooler is chilled to 40 ℃ to be mixed with inverse put gas phase.Pressure process is by drop to-0.085MPa of 0.02MPa.
Two equal voltage rise E2R
In adsorption tower D, gas flows into adsorption tower A, carries out isostasy, and when two pressure towers equate substantially, this step finishes.
One equal voltage rise E1R
In adsorption tower E, gas flows into adsorption tower A, carries out isostasy, and when two pressure towers equate substantially, this step finishes.
FR finally boosts
Absorption waste gas enters adsorption tower A and finally boosts.When adsorption tower A pressure approaches adsorptive pressure substantially, this step finishes.
So far, all eight steps of adsorption tower A in one-period are all finished, and start to enter next time circulation, and the performed step of other seven adsorption towers is identical with adsorption tower A, just mutually stagger in time, to guarantee that separation process carries out continuously.
Each adsorption column pressure is cyclically-varying with the variation of processing step, and according to practical operation situation, adsorptive pressure can suitably be adjusted, other step pressure is corresponding changes.
The separated Adsorption Phase product reclaiming forms as shown in table 5:
Table 5
。
Recovery rate of ethylene 95%
Embodiment 2
The present embodiment is the separated pressure swing adsorption method that reclaims carbon dioxide from synthetic-ammonia transformation gas, the about 15000Nm of mixed gas flow
3/ h, the about 0.75Mpa of adsorptive pressure, approximately 30 ℃ of temperature, processed mixed gas composition forms as shown in table 1:
Table 1 unstripped gas forms
。
The present embodiment pressure swing adsorption system consists of 1 section of PSA-1 of pressure-variable adsorption, 2 sections of PSA-2 of pressure-variable adsorption and 3 sections of PSA-3 of pressure-variable adsorption.Unstripped gas enters 1 section of pressure-variable adsorption, the displacement waste gas that pressure-variable adsorption is 1 section enters 2 sections of unstripped gas as 2 sections of pressure-variable adsorptions of pressure-variable adsorption, from 1 section of pressure-variable adsorption, obtain carbon dioxide product and displacement gas with inverse put gas and the exhaust of 2 sections of pressure-variable adsorptions, the absorption waste gas that 1 section of pressure-variable adsorption and pressure-variable adsorption are 2 sections enters 3 sections of unstripped gas as 3 sections of pressure-variable adsorptions of pressure-variable adsorption, after the inverse put that pressure-variable adsorption is 3 sections and exhaust supercharging, returning to 1 section of pressure-variable adsorption mixes with unstripped gas as 1 section of unstripped gas of pressure-variable adsorption, the absorption waste gas output device that pressure-variable adsorption is 3 sections goes recover hydrogen or as fuel gas.
PSA-1 is formed by connecting by 8 adsorption towers and corresponding pipeline.Every tower experience absorption A, that circulates each time all falls E1D, two and all falls E2D, displacement RP, the reverse D of bleeding off pressure, the V that finds time, two and all rise E2R, and all rise E1R, final nine steps of FR of boosting, and its program operation sequential is in Table 2-1.
Table 2-1
。
Install flow chart as shown in Figure 1:
Each adsorption tower experiences following steps successively according to the listed sequential of table 2:
So far, the institute of adsorption tower A in one-period is all finished in steps, and starts to enter next time circulation, and the performed step of other 7 adsorption towers is identical with adsorption tower A, just mutually staggers in time, to guarantee that separation process carries out continuously.
Each adsorption column pressure is cyclically-varying with the variation of processing step, and according to practical operation situation, adsorptive pressure can suitably be adjusted, other step pressure is corresponding changes.
PSA-2 is comprised of 4 adsorption towers and corresponding pipeline is formed by connecting.Every tower circulate each time all experience absorption A, all pressure drop ED, displacement RP, the reverse D of bleeding off pressure, the V that finds time, all voltage rise ER, final seven steps of FR of boosting, its program operation sequential is in Table 2-2.The circulation step of each tower experience is as listed in table 2-2 time-scale:
Table 2-2 PSA-2 time-scale
。
So far, the institute of adsorption tower I in one-period is all finished in steps, and starts to enter next time circulation, and the performed step of other 3 adsorption towers is identical with adsorption tower I, just mutually staggers in time, to guarantee that separation process carries out continuously.
PSA-3 is formed by connecting by 8 adsorption towers and corresponding pipeline.Every tower experience absorption A, that circulates each time all falls E1D, two and all falls E2D, the reverse D of bleeding off pressure, the V that finds time, two and all rise E2R, and all rise E1R, final nine steps of FR of boosting, and its program operation sequential is in Table 2-3.
Table 2-3 PSA-3 work schedule table
。
Each adsorption column pressure is cyclically-varying with the variation of processing step, and according to practical operation situation, adsorptive pressure can suitably be adjusted, other step pressure is corresponding changes.The separated Adsorption Phase product reclaiming forms as shown in table 3:
Table 3 gas product forms
。
Claims (8)
1. a pressure swing absorption process that improves Adsorption Phase product recovery rate, it is characterized in that, this pressure swing adsorption system comprises 3 sections of 1 section of pressure-variable adsorption and 2 sections of pressure-variable adsorptions and pressure-variable adsorptions, every section of pressure-variable adsorption consists of at least two adsorption towers that are filled with adsorbent respectively, each adsorption tower that 1 section of pressure-variable adsorption and pressure-variable adsorption are 2 sections circulates at least successively and experiences absorption, displacement, find time, the step of boosting, and the displacement waste gas that pressure-variable adsorption is 1 section enters 2 sections of pressure-variable adsorptions as unstripped gas, each adsorption tower that pressure-variable adsorption is 3 sections circulates at least successively and experiences absorption, inverse put, the step of boosting, or the absorption of circulation experience at least successively, find time, the step of boosting, the absorption waste gas that pressure-variable adsorption is 1 section is as the unstripped gas of 3 sections of pressure-variable adsorptions, enter 3 sections of pressure-variable adsorptions, after the inverse put gas that pressure-variable adsorption is 3 sections and exhaust supercharging, mix with the unstripped gas of 1 section of pressure-variable adsorption as unstripped gas and introduce 1 section of pressure-variable adsorption.
2. pressure swing absorption process according to claim 1, is characterized in that the unstripped gas of 2 sections of pressure-variable adsorptions can also comprise the displacement waste gas of 2 sections of pressure-variable adsorptions.
3. pressure swing absorption process according to claim 1 and 2, is characterized in that, the absorption waste gas that the absorption waste gas that described pressure-variable adsorption is 1 section and pressure-variable adsorption are 2 sections is introduced 3 sections of unstripped gas as 3 sections of pressure-variable adsorptions of pressure-variable adsorption.
4. pressure swing absorption process according to claim 1 and 2, it is characterized in that, according to raw gas pressure and displacement gas pressure, increase the one or more of the following step, after the adsorption step of 2 sections of 1 section of pressure-variable adsorption and pressure-variable adsorptions, increase by 1 time or equal voltage drop step repeatedly, after displacement step, increase by 1 time or equal voltage drop step repeatedly, before evacuation step, increase inverse put step, after evacuation step, increase the equal voltage rise step of one or many; 3 sections of pressure-variable adsorptions circulation experience successively absorption, inverse puts, the steps of finding time, boost, and after adsorption step, increase by 1 time or equal voltage drop step repeatedly, the equal voltage rise step of one or many before the step of boosting, increased; The inverse put gas that pressure-variable adsorption is 3 sections and exhaust return to 1 section of unstripped gas as 1 section of pressure-variable adsorption of pressure-variable adsorption.
5. pressure swing absorption process according to claim 1 and 2, is characterized in that, inverse put gas, exhaust that 1 section of described pressure-variable adsorption and pressure-variable adsorption are 2 sections are Adsorption Phase product.
6. pressure swing absorption process according to claim 1 and 2, is characterized in that, is the displacement gas of 2 sections of 1 section of pressure-variable adsorption and pressure-variable adsorptions after the inverse put gas that 1 section of part pressure-variable adsorption and pressure-variable adsorption are 2 sections, exhaust supercharging.
7. pressure swing absorption process according to claim 1 and 2, it is characterized in that, the adsorption step pressure that described pressure-variable adsorption is 1 section is greater than 0.15MPa, the adsorption step pressure that 2 sections of pressure-variable adsorptions and pressure-variable adsorption are 3 sections is greater than 0.1Mpa, displacement step pressure is greater than 0.1Mpa, inverse put step pressure is greater than 0.1Mpa, and evacuation step pressure is 0.001～0.07MPa; Described pressure is absolute pressure.
8. pressure swing absorption process according to claim 1 and 2, is characterized in that, the described separated Adsorption Phase product reclaiming is carbon dioxide, carbon monoxide and hydrocarbon component, and described hydrocarbon component is methane, ethene, ethane and C
3above component.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210394237.3A CN102935324B (en) | 2012-10-17 | 2012-10-17 | Variable pressure absorption method for increasing absorption phase product yield |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210394237.3A CN102935324B (en) | 2012-10-17 | 2012-10-17 | Variable pressure absorption method for increasing absorption phase product yield |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102935324A CN102935324A (en) | 2013-02-20 |
| CN102935324B true CN102935324B (en) | 2014-07-16 |
Family
ID=47694264
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210394237.3A Active CN102935324B (en) | 2012-10-17 | 2012-10-17 | Variable pressure absorption method for increasing absorption phase product yield |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102935324B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104624017B (en) * | 2015-01-23 | 2019-04-30 | 四川省达科特能源科技股份有限公司 | The method of lighter hydrocarbons is recycled in a kind of natural gas, associated gas |
| CN106256409B (en) * | 2016-08-21 | 2019-09-03 | 杭州东安科技有限公司 | A kind of pressure swing adsorption system |
| CN110354637B (en) * | 2019-07-30 | 2021-12-10 | 盖氏科技 | Method for enriching easily-adsorbed gas by pressure swing adsorption method |
| EP4137451A4 (en) * | 2020-04-14 | 2024-01-17 | Chengdu Yingchen Tech Co Ltd | Method of movable pressure swing adsorption oxygen production device |
| CN115155246A (en) * | 2022-08-10 | 2022-10-11 | 北京佳安氢源科技股份有限公司 | Low-concentration hydrogen adsorption purification method |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5133785A (en) * | 1991-02-26 | 1992-07-28 | Air Products And Chemicals, Inc. | Separation of multicomponent gas mixtures by selective adsorption |
| CN1243597C (en) * | 2004-01-18 | 2006-03-01 | 成都天立化工科技有限公司 | Process for removing CO2 from conversion gas by three-stage pressure swing adsorption device |
| CN100423811C (en) * | 2005-10-01 | 2008-10-08 | 四川天一科技股份有限公司 | Pressure-variation absorption method for separating and recovering adsorbed phase products from mixed gas |
-
2012
- 2012-10-17 CN CN201210394237.3A patent/CN102935324B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN102935324A (en) | 2013-02-20 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104147896B (en) | Two-stage nitration pressure-variable adsorption reclaims the method for absorption phase product | |
| CN102935324B (en) | Variable pressure absorption method for increasing absorption phase product yield | |
| CN106693608B (en) | A kind of process for separating and recovering of oil refinery dry gas | |
| CN100423811C (en) | Pressure-variation absorption method for separating and recovering adsorbed phase products from mixed gas | |
| CN102245500B (en) | Production of hydrogen from a reforming gas and simultaneous capture of CO2 co-product | |
| CN104058371A (en) | Pressure swing adsorption gas production system and pressure swing adsorption gas production method | |
| CN105026528B (en) | Methane gas method for concentration | |
| CN101978235A (en) | Method and apparatus for separating blast furnace gas | |
| CN103801171B (en) | A kind of two-stage series connection swing adsorption oxygen generating system and method for operating thereof improving oxygen recovery rate | |
| CN103170214B (en) | Method for recovering methane chloride from organic silicon synthetic tail gas | |
| CN203724982U (en) | Two-stage series pressure swing adsorption oxygen generation system capable of improving oxygen recovery rate | |
| CN103585856A (en) | Multi-backflow pressure swing adsorption method | |
| CN101643209A (en) | Method for purifying and reclaiming carbon dioxide from landfill gas and device thereof | |
| CN104986735B (en) | A kind of method for improving hydrogen recovery rate | |
| CN85103557A (en) | Methane in the pressure swing adsorption method enrichment coal mine mash gas | |
| CN103068778B (en) | Method and apparatus for recovering ethylene from fluidized catalytic cracking (fcc) off-gas | |
| CN103861422A (en) | New technique for concentrating methane in oxygen-containing coal bed gas | |
| CN101732947B (en) | Method for safe adsorption and enrichment of gas with low concentration | |
| CN107759436B (en) | Method for preparing high-purity methane by adsorbing and separating methane nitrogen through simulated moving bed | |
| CN107774096B (en) | A kind of method of Quan Wencheng sorption extraction recycling polyolefin tail hydro carbons | |
| CN104740972A (en) | Pressure swing adsorption gas separation method for recycling displacement waste gas and directly-discharged gas | |
| CN205235699U (en) | Purifier of adsorption tower and LNG feed gas | |
| CN102009963A (en) | High-purity nitrogen preparing method and device | |
| CN103695063B (en) | Method for concentrating low-concentration methane gas | |
| CN1040354A (en) | Pressure swing adsorption process extracts carbonic acid gas from gas mixture |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address |
Address after: 610225 Technology Innovation Service Center of Chengdu High-tech Zone, Chengdu, Sichuan Province, No. 5 Gaopeng Avenue, Chengdu High-tech Zone Patentee after: Haohua Chemical Technology Group Co., Ltd. Address before: 610225 Technology Innovation Service Center of Chengdu High-tech Development Zone, No. 5 Gaopeng Avenue, Chengdu High-tech Development Zone, Sichuan Province Patentee before: Tianyi Science and Technology Co., Ltd., Sichuan Prov |
|
| CP03 | Change of name, title or address | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20200423 Address after: No. 5 high tech Zone Gaopeng road in Chengdu city of Sichuan Province in 610041 Patentee after: SOUTHWEST RESEARCH & DESIGN INSTITUTE OF CHEMICAL INDUSTRY Address before: 610225 Technology Innovation Service Center of Chengdu High-tech Zone, Chengdu, Sichuan Province, No. 5 Gaopeng Avenue, Chengdu High-tech Zone Patentee before: Haohua Chemical Technology Group Co., Ltd. |
|
| TR01 | Transfer of patent right |