CN1215624A - Multi-bed vacuum pressure swing adsorption process for extracting hydrogen from hydrogen-contg. mixed gas - Google Patents
Multi-bed vacuum pressure swing adsorption process for extracting hydrogen from hydrogen-contg. mixed gas Download PDFInfo
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- CN1215624A CN1215624A CN 97107735 CN97107735A CN1215624A CN 1215624 A CN1215624 A CN 1215624A CN 97107735 CN97107735 CN 97107735 CN 97107735 A CN97107735 A CN 97107735A CN 1215624 A CN1215624 A CN 1215624A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40058—Number of sequence steps, including sub-steps, per cycle
- B01D2259/40066—Six
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/402—Further details for adsorption processes and devices using two beds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/406—Further details for adsorption processes and devices using more than four beds
Abstract
A pressure-swing adsorption process for extracting and purifying hydrogen from hydrogen-containing mixed gas containing high-hydrocarbons impurities features that in the pressure-swing adsorption system with at least two adsorption beds, the adsorbent filled in the adsorption beds can selectively adsorb the impurities in mixed gas to prepare hydrogen with purity of 98-99.999% and recovery of 90-95%. Each bed is subjected to adsorption, homogenizing pressure drop, reverse pressure reduction, vacuumizing or vacuumizing plus flushing, homogenizing pressure raise and final raising pressure.
Description
The present invention relates to from the hydrogen-containing gas mixture to separate and the method for purified gases, particularly close H from refinery gas etc.
2And C
5The transformation of purified hydrogen absorption (PSA) technology in the gas mixture of above high hydrocarbon component.
Adopt pressure swing adsorption process from closing the hydrogen gas mixture,, successfully be widely used in fields such as chemical industry, electronics, plant produced has been played energy-saving and cost-reducing unusual effect such as pure hydrogen of middle extraction such as ammonia factory off-gas.At United States Patent (USP) 3,564, in 816, the four two equal adiabatic pressure swing adsorption techniques of being narrated have been widely used in from the gaseous mixture of impurity such as hydrogeneous and water, carbonic acid gas, methane, carbon monoxide, for example separation of hydrogen in the petroleum naphtha steam reforming gas.But this technology is subjected to the restriction of maximum bed size, causes adsorption bed throughput to be restricted.If solve this problem with the method that is equipped with two cover systems, but the low and big problem of sorbent material consumption of the hydrogen rate of recovery appears.United States Patent (USP) 3,986 for this reason, and 849 have proposed to adopt the adiabatic pressure swing adsorption process of many selection absorption.
Above-mentioned United States Patent (USP) 3,986,8849 has been put down in writing ten three equal technologies of PSA of extracting hydrogen from unstripped gas, the main ingredient of its unstripped gas:
Component: H
2CO CO
2CH
4
V％：?????69.22????3.57????20.92????6.29
Unstripped gas is at pressure 2.5MPa, enters the equal technology PSA of ten three of above-mentioned United States Patent (USP) system under 40 ℃.The loop cycle of each adsorption bed by absorption A, once all pressure drop E1D, the equal pressure drop E2D of secondary, three equal pressure drop E3D, forward step-down PP, reverse step-down RD, flushing P, three equal voltage rise E3R, the equal voltage rise E2R of secondary, once all voltage rise E1R, finally the FR that boosts constitutes.When ten bed operatings, always there are three adsorption beds to be in the step of product, all the other seven adsorption beds are in the regenerated different step.Table 2 has been listed the time and the pressure change of each processing step in each loop cycle.This technology is optionally adsorbed Ar, N from the rich hydrogen unstripped gas with elevated pressures
2Or impurity such as CO, obtain high purity product hydrogen.Through the improvement of this patent, product recovery rate is increased, its rate of recovery is brought up to about 85% by 80%; Output is not subjected to the restriction of adsorption bed size; The cumulative volume of adsorption bed and sorbent material consumption all reduce to some extent than the method in past.The invention of this patent is maximized transformation absorption and is become a reality.
But enterprising patent is to adopt product hydrogen process of washing to come these impurity of desorption to the regeneration of the sorbent material that adsorbed impurity, thus this partly hydrogen can't reclaim, and the yield of product can not further be improved.
According to rate of recovery calculation formula:
R=Xp(Xf-Xw)/Xf(Xp-Xw)
In the formula: R is the rate of recovery, and Xp is a hydrogen content in the product hydrogen, and Xf is a hydrogen content in the unstripped gas, and Xw is a hydrogen content in the waste gas.
Formula shows, what of amounts of hydrogen directly influence the PSA rate of recovery in the waste gas, so two steps are being washed and discharged to the loss of hydrogen mainly.According to a routine unstripped gas treatment capacity is 70000Nm
3/ h, convert for every adsorption bed weekly the phase treatment capacity be 1555.6Nm
3/ phase platform weekly, the product work output is 411866Nm
3/ h, convert for every adsorption bed weekly the phase output products be 915.2Nm
3/ phase platform is weekly calculated, and is being 146.6Nm along the amounts of hydrogen that is used to wash by adsorption bed output in rapid of strideing
3/ h/ is the phase platform weekly, and the rate of recovery of its hydrogen only is 84.9% hydrogen.
In addition, for some high hydro carbons adsorbate, poor effect also will be carried out pre-treatment to unstripped gas for this reason before transformation absorption with hydrogen flushing reproducing adsorbent.
Given this, the object of the present invention is to provide a kind of multi-bed vacuum pressure swing adsorption process that from hydrogeneous gas mixture, extracts hydrogen that can further improve product recovery rate, reduce the sorbent material consumption.
Another object of the present invention provides a kind of multi-bed vacuum pressure swing adsorption process that extracts hydrogen from hydrogeneous gas mixture of removing high hydrocarbon impurities, process simplification, facility investment reduction.
The present invention adopts to vacuumize step, the rinse step in all or part of alternative prior art based on prior art.Thereby, not only make the present invention from the refinery gas that contains high hydro carbons, extract hydrogen; And can be all or reduce flushing dose significantly, reducing with step-down gas forward bed is washed the product hydrogen loss that causes, the cancellation pretreatment system with this consumption that improves the product hydrogen rate of recovery and reduce sorbent material, is realized its purpose.
The multi-bed vacuum pressure swing adsorption process that from hydrogeneous gas mixture, extracts hydrogen of the present invention, in the pressure swing adsorption system of at least two adsorption beds is arranged, optionally adsorb the impurity in the gas mixture and produce hydrogen with the sorbent material that is filled in the adsorption bed, it is characterized in that experience absorption successively, all pressure drop, the reverse step-downs in circulation once of each adsorption bed, add flushing in vacuumizing or vacuumizing, equal voltage rise, the final step of boosting.
The above-mentioned step of finally boosting is adsorption bed finally to be boosted from the product end with product gas, or simultaneously adsorption bed is finally boosted from the product end from feed end and product gas with unstripped gas.
Above-mentioned sorbent material can be at least a in zeolite molecular sieve, gac, silica gel, the activated alumina.
The pressure of above-mentioned adsorption step is 0.6～3.5MPa.
The above-mentioned pressure that vacuumizes step is-0.03～-0.09MPa.
The multi-bed vacuum pressure swing adsorption process that extracts hydrogen from hydrogeneous gas mixture of the present invention, in pressure swing adsorption system, unstripped gas is a gas mixture, enters adsorption bed under 20～40 ℃ of 0.6～3.5MPa pressure, room temperature.The sorbent material of filling has zeolite molecular sieve, gac, silica gel, activated alumina etc. in the adsorption bed, can adorn a kind ofly separately according to the component of unstripped gas, and the sorbent material that also can adorn two or more in proportion constitutes multiple-hearth; The quantity of adsorption bed can be selected two to 12 according to tolerance, pressure, it can be six, seven, eight, nine, ten, 12 etc., and be equipped to once to six equal pressure drops and all voltage rises, can be secondary or three times, four times so that five times, six equal pressure drops and all voltage rises constitute many repeatedly equal compression technologies.Form circulation by many repeatedly equal compression technology steps, make the intermittent process serialization of adsorbent reactivation.Each adsorption bed experiences following steps successively in once circulating:
(1) absorption (A):
Unstripped gas constantly enters adsorption bed under the constant adsorptive pressure, simultaneously output products hydrogen.In adsorption step, sorbent material in the adsorption bed is passed in time the hold-up of the impurity composition beyond the hydrogen and is progressively increased, stop incoming stock gas when arriving the hold-up of regulation, absorption stops, and still is reserved with the sorbent material that a part is not adsorbed impurity this moment in the adsorption bed.
(2) all pressure drop is that pressure equalization is fallen:
Direction along incoming stock gas output products hydrogen reduces pressure, and effluent air is a product hydrogen still, is used for other adsorption bed and boosts.This eluting gas can be respectively applied for different several adsorption beds and boost, thereby can form repeatedly the equal pressure drop stage, can be once all pressure drops (E1D), the equal pressure drop of secondary (E2D), three equal pressure drops (E3D), four equal pressure drops (E4D), five equal pressure drops (E5D), six equal pressure drops (E6D) ...In this process, constantly descend with the implantation internal pressure, the impurity on the sorbent material is by constantly desorb, it is adsorbed that impurity after the desorb continues not adsorbed the sorbent material of impurity again, therefore impurity does not leave adsorption bed, and along with step-down is carried out, the agent of final bed internal adsorption is all taken by impurity.
(3) reverse step-down (D):
Direction against incoming stock gas output products hydrogen reduces pressure, and until barometric point, the impurity of most of occlusion is discharged outside the adsorption bed with air-flow in the adsorption bed.Reverse depressurization step can be finished several times, is called once reverse step-down (D1), the reverse step-down of secondary (D2) ...
(4) vacuumize (VC):
Reverse step-down finishes in the adsorption bed of back still some impurity hold-up, for making the desorb as far as possible of this part impurity, require the bed internal pressure further to reduce, utilize the method for vacuum pump suction to reduce impurities partial pressure, make the impurity desorb and take adsorption bed out of, according to the composition of unstripped gas, particularly when containing the component that is difficult to desorb such as heavy hydrocarbon in the unstripped gas with vacuumizing gas, the composition situation of visual its component during vacuumizing, or increase an amount of flushing or do not increase flushing.
(5) all voltage rise is the pressure equalization liter:
Adsorption bed after vacuumizing desorption and regeneration is in the minimal pressure of technological process, utilizes product hydrogen that the corresponding adsorption bed that is in equal voltage drop step discharges to enter adsorption bed from the product end of this adsorption bed under this pressure condition and makes it progressively to raise pressure.All voltage rise can be finished several times, forms repeatedly all voltage rise stages, is called ... six equal voltage rises (E6R), five equal voltage rises (E5R), four equal voltage rises (E4R), three equal voltage rises (E3R), the equal voltage rise of secondary (E2R), once all voltage rises (E1R).
(6) (FR) finally boosts:
Because all the voltage rise step can't make adsorbent beds arrive adsorptive pressure, therefore the part of the product hydrogen that need export with the adsorption bed that is in adsorption step is boosted to this adsorption bed from the product output terminal, also can finally boost to adsorption bed simultaneously from the product end from feed end and product gas, until reaching adsorptive pressure with unstripped gas.
The step of finally boosting is adsorption bed finally to be boosted from the product end with product gas, or simultaneously adsorption bed is finally boosted from the product end from feed end and product gas with unstripped gas.
It is main ingredient that the present invention is specially adapted to separate with hydrogen, and contains CO, CO
2, lightweight or heavy hydrocarbon, the gas mixture of lightweight sulfide, nitrogen and water is such as petroleum reforming gas, hydrocracking gas, conversion gas etc.
The multi-bed vacuum pressure swing adsorption process that extracts hydrogen from hydrogeneous gas mixture of the present invention, compared with the prior art, particularly with United States Patent (USP) 3,564,816 and 3,986,849 compare and have following obvious advantage and unusual effect.
One, the present invention is with vacuumizing step, replaces the rinse step of prior art and depressurization step forward, and formation multi-bed vacuum pressure swing adsorption technique.This improved benefit is to have avoided the product loss that causes because of flushing, thereby has improved the rate of recovery of product gas significantly and reduced the consumption of sorbent material.This improvement is for the PSA device that maximizes, and its effect is appreciable.
Two, the present invention adopts vacuum step to replace the rinse step of prior art, be-0.03 in vacuum tightness～-0.09MPa pressure under, can make C
5Above high hydrocarbon component only needs a step process just to be desorbed, and need not carry out pre-treatment.This be because this class gas mixture to adopt the rinse step of existing pressure swing absorption process be can't be C
5High hydrocarbon impurities desorbs from sorbent material fully, need adopt usually to add alternating temperature absorption and carry out pre-treatment and remove before entering transformation absorption, has so just increased the complicacy and the investment cost of equipment of technical process.
Therefore, the present invention is specially adapted to from containing high hydro carbons (C
5More than) rich hydrogen gas mixture, as refinery gas, comprise and extract pure hydrogen in hydrocracking gas, the petroleum reforming hydrogen rich gas etc., and can simplify the system device of technology, reduce facility investment and production cost.
Adopt pressure swing adsorption process of the present invention purifying hydrogen of hydrogen from the gas mixture that is rich in hydrogen and high hydro carbons, can obtain product H
2Be 98～99.999%, H
2The rate of recovery be 90～95% pure hydrogen.Compare with existing PSA technology, the rate of recovery of hydrogen can improve about 10%.This shows, use PSA technology of the present invention, both can be fit to contain the rich hydrogen gas mixture purified hydrogen of heavy hydrocarbons impurity, can improve the rate of recovery of product hydrogen again.And people also will appreciate that the power consumption that increases for vacuumizing, and are remedied by the sorbent material consumption of the product yield of its increase and minimizing and the pre-processing device save for the purification of handling the heavy hydrocarbons hydrogen source.
Below, with embodiment and accompanying drawing thereof the present invention is further described again.
Brief description of drawings.
Fig. 1 is a kind of process flow sheet that extracts the multi-bed vacuum pressure swing adsorption process of hydrogen from hydrogeneous gas mixture of the present invention.Show ten four equal technical process.
Fig. 2 is another kind of the present invention extracts the multi-bed vacuum pressure swing adsorption process of hydrogen from hydrogeneous gas mixture a process flow sheet.Show six two equal technical process.
Embodiment 1
A kind of multi-bed vacuum pressure swing adsorption process that extracts hydrogen from hydrogeneous gas mixture of the present invention is a purifying hydrogen of hydrogen the gas mixture from following unstripped gas.
Unstripped gas is the low gas mixture that divides dry gas of CONTINUOUS REFORMER hydrogen rich gas, hydrocracking dry gas, hydrofining of refinery, its composition: H
2N
2CH
4C
2C
3I-C
4N-C
4N-C
5C
+ 686.30 0.07 4.74 3.61 3.11 1.12 0.61 0.27 0.16
This pressure swing adsorption process is formed according to above-mentioned raw materials, really with ten four equal pressure swing adsorption systems shown in Figure 1.This system is made up of with the pipeline that is connected with each adsorber, program valve etc. ten adsorbers of making adsorption bed.Above-mentioned adsorber is divided into single series adsorber 1,3,5,7,9 and bi serie adsorber 2,4,6,8,10.Molecular sieve gac that loads in ten adsorbers and activated alumina are by common proportional layered filling.With adsorber 1,2,3,4,5,6,7,8,9, dispose unstripped gas entry program valve 101 in 10 corresponding pipeline that are connected respectively, 102,103,104,105,106,107,108,109,110, product hydrogen export procedure valve 201,202,203,204,205,206,207,208,209,210, reverse emptying program valve 301,302,303,304,305,306,307,308,309,310, all press program valve 401 four times, 402,403,404,405,406,407,408,409,410, once all press and the program valve 501 that finally boosts, 502,503,504,505,506,507,508,509,510, two, all press program valve 601 three times, 602,603,604,605,606,607,608,609,610, the program of finding time valve 701,702,703,704,705,706,707,708,709,710, variable valve HV-102 finally boosts.
Unstripped gas is at pressure 1.28MPa, and temperature enters native system for 30～40 ℃, from bottom to up by being in each adsorber of adsorption step, when system moves, presses each program valve of programming Control by computer by inlet end.The loop cycle of each adsorption bed by absorption A, once all pressure drop E1D, the equal pressure drop E2D of secondary, three equal pressure drop E3D, four equal pressure drop E4D, once reverse step-down D1, the reverse step-down D2 of secondary, vacuumize VC, four equal voltage rise E4R, three equal voltage rise E3R, the equal voltage rise E2R of secondary, once all voltage rise E1R, finally 13 steps of FR of boosting are formed.Table 1 has been listed the mutual relationship that ten adsorbers respectively go on foot preface.Be in operation, always have three adsorption beds to be in the adsorption step of incoming stock gas, output hydrogen, all the other seven adsorption beds are in the different step of adsorbent reactivation; The step of finally boosting adopts product gas from the product end adsorption bed finally to be boosted, or adopts unstripped gas simultaneously adsorption bed finally to be boosted from the product end from feed end and product gas.Strong adsorbent component in the adsorber in the adsorbents adsorb unstripped gas of filling, the hydrogen component with weak adsorptivity is emitted from exit end as product, at pressure 1.18MPa, transports to the user under temperature≤40 ℃.
Step is pressed and vacuumized to the stripping gas of pressure swing adsorption system from reverse putting, and vacuumizing the stripping gas of step by the vacuum pump suction, at pressure 0.01～0.02MPa, under temperature≤40 ℃, is sent to follow-up stripping gas system.
About 800 seconds of the circulation time that system's operation is experienced, its time distributes with the pressure change of each algorithm as shown in table 2.The pressure of adsorption step shown in the table 2 is 1.2MPa, and the pressure that vacuumizes step is-0.08MPa.
The purity that present embodiment can obtain product hydrogen is 99.9%, and the rate of recovery of hydrogen is 90%.
Embodiment 2:
Another kind of the present invention extracts the multi-bed vacuum pressure swing adsorption process of hydrogen from hydrogeneous gas mixture, be purifying hydrogen of hydrogen the gas mixture from following unstripped gas.
Unstripped gas is an ammonia factory conversion gas, and its typical case forms:
Component: H
2CH
4+ Ar+N
2CO CO
2
V％：?????52????～18?????～2???～28
This pressure swing adsorption process is formed according to above-mentioned raw materials, adopts six two equal pressure swing adsorption systems shown in Figure 2.This pressure swing adsorption system is made up of six adsorber A, B, C, D, E, F and the pipeline that is connected with each adsorber, program valves etc. of making adsorption bed.With corresponding pipeline that adsorber A, B, C, D, E, F are connected in dispose unstripped gas entry program valve 1A, 1B, 1C, 1D, 1E, 1F respectively, product hydrogen export procedure valve 2A, 2B, 2C, 2D, 2E, 2F, reverse emptying program valve 3A, 3B, 3C, 3D, 3E, 3F, secondary is all pressed program valve 4A, 4B, 4C, 4D, 4E, 4F, program valve 5A, 5B, 5C, 5D, 5E, 5F once all press and finally boost, evacuation valve 6A, 6B, 6C, 6D, 6E, 6F, variable valve FG102 finally boosts.
During the operation of this pressure swing adsorption system, press each program valve of programming Control by computer, unstripped gas is at pressure 1.2MPa, enter pressure swing adsorption system under 30～40 ℃ of the temperature, from bottom to top by being in the adsorber of adsorption step, the processing step of listing by table 3 moves unstripped gas by inlet end in the pressure swing adsorption system.Each loop cycle of each adsorption bed by absorption A, once all pressure drop E1D, the equal pressure drop E2D of secondary, once reverse step-down D1, the reverse step-down D2 of secondary, vacuumize VC, the equal voltage rise E2R of secondary, once all voltage rise E1R, finally nine steps of FR of boosting are formed.The step of finally boosting adopts product gas from the product end adsorption bed finally to be boosted, or adopts unstripped gas simultaneously adsorption bed finally to be boosted from the product end from feed end and product gas.In service always have two adsorbers to be in adsorption step, to guarantee that unstripped gas enters adsorption bed continuously, the output of product stabilized hydrogen.Desorb by reverse put to calm the anger and vacuumize gas form.About 650 seconds of the cycling time that each cycle is experienced.Its time distributes with the pressure such as the table 4 of each algorithm listed.The pressure of adsorption step shown in the table is 1.25MPa; The pressure that vacuumizes step is-0.08MPa.
Present embodiment, can obtain purity is 99.9%, the rate of recovery is greater than 95% pure hydrogen.Compare with existing above-mentioned United States Patent (USP), can improve the product hydrogen rate of recovery 10.1%.
Ten four equal processing steps of table 1 PSA of the present invention
| Divide the cycle | ????1 | ????2 | ????3 | ????4 | ????5 | ????6 | ????7 | ????8 | ????9 | ????10 | |||||||||||
| Adsorption bed | ?1 ?2 ?3 ?4 ?3 ?6 ?7 ?8 ?9 ?10 | ????A | ?EIR | ?E2D | ?E3D | ?E4D | ?D | ????VC | ?E4R | ?E3R | ?E2R | ?E1R | ?FR | ||||||||
| ?E1R | ?FR | ????A | ?EID | ?E2D | ?E3D | ?E4D | ????D | ????VC | ?E4R | ?E3R | ?E2R | ||||||||||
| ?E3R | ?E2R | ?E1R | ?FR | ????A | ?E1D | ?E2D | ?E3R | ?E4D | ?D | ????VC | ?E2R | ||||||||||
| ?VC | ?E4R | ?E3R | ?E2R | ?E1R | ?FR | ?????????????????????????????A | ?E1R | ?E2D | ?E3D | ?E4D | ?D | ????VC | |||||||||
| ????VC | ?E4R | ?E3R | ?E2R | E1R | ?FR | ??????????????????????????????A | ?E1D | ?E2D | ?E3D | ?E4D | ?D | ?VC | |||||||||
| ????D | ????VC | ?E4R | E3R | ?E2R | ?E1R | ?FR | ????A | ?E1D | ?E2D | ?E3D | ?E4D | ||||||||||
| ?E2D | ?E4D | ?D | ????VC | ?E4R | ?E3R | ?E2R | ?E1R | ?FR | ????A | ?E1D | ?E2D | ||||||||||
| ?E1D | ?E2D | ?E3D | ?E4D | ?D | ????VC | ?E4R | ?E3R | ?E2R | ?E1R | ?FR | ????A | ||||||||||
| ????A | ?E1D | ?E2D | ?E3D | ?E4R | D | ??????????????????VC | ?E4R | ?E3R | ?E2R | ?E1R | ?FR | ?????????????????A | |||||||||
| ????A | ?E1D | ?E2D | E3D | ?E4D | ?D | ?????????????????VC | ?E4R | ?E3R | ?E2R | ?E1R | ?FR | ??????????A | |||||||||
Time, the pressure distribution of ten four equal each step of technology of table 2 PSA of the present invention
| Algorithm | ????A | ????E1D | ????E2D | ????E3D | ????E4D | ????D1 | ????D2 | ????VC | ????E4R | ?E3R | ?E2R | ?E1R | ?FR |
| Time (second) | ????24 | ????30 | ????39 | ????37 | ????37 | ????14 | ????25 | ????158 | ????37 | ?37 | ?39 | ?30 | ?48 |
| Pressure (MPa) | ????12 | ????0.98 | ????0.7 | ????0.43 | ????0.17 | ????0.05 | ????0.02 | ????-0.08 | ????0.17 | ?0.43 | ?0.7 | ?0.98 | ?1.25 |
Six two equal processing steps of table 3 PSA of the present invention
| Divide the cycle | ????1 | ????2 | ????3 | ????4 | ????5 | ????6 | |||||||
| Adsorption bed | ?A | ????A | ?E1D | ?E2D | ?D | ????VC | ?E2R | ?E1R | ?FR | ||||
| ?B | ?E1D | ?FR | ??????????????A | ?E1D | ?E2D | ?D | ????VC | ?E2R | |||||
| ?C | ?VC | ?E2R | ?F1R | ?FR | ????A | ?E1D | ?E2D | ?D | ?VC | ||||
| ?D | ?D | ??????VC | ?E2R | ?E1R | ?FR | ????A | ?E1D | ?E2D | |||||
| ?E | ?E1D | ?E2D | ?D | ??????VC | ?E2R | ?E1R | ?FR | ????A | |||||
| ?F | ????A | ?E1D | ?E2D | ?D | ?????VC | ?E2R | ?E1R | ?FR | ????A | ||||
Time, the pressure distribution of six two equal each step of technology of table 4 PSA of the present invention
| Algorithm | ????A | ????E1D | ????E2D | ????D1 | ????D2 | VC | ?E2R | ????E1R | ????FR |
| Time (second) | ????220 | ?30 | ????64 | ????16 | ????25 | 108 | ?64 | ????30 | ????78 |
| Pressure (MPa) | ????1.25 | ?0.81 | ????0.36 | ????0.05 | ????0.02 | -0.08 | ?0.3 | ????0.81 | ????1.25 |
Claims (4)
1, from hydrogeneous gas mixture, extracts the multi-bed vacuum pressure swing adsorption process of hydrogen, in the pressure swing adsorption system of at least two adsorption beds is arranged, optionally adsorb the impurity in the gas mixture and produce hydrogen with the sorbent material that is filled in the adsorption bed, it is characterized in that experience absorption successively, all pressure drop, the reverse step-downs in circulation once of each adsorption bed, add flushing in vacuumizing or vacuumizing, equal voltage rise, the final step of boosting.
2, the multi-bed vacuum pressure swing adsorption process that from hydrogeneous gas mixture, extracts hydrogen according to claim 1, it is characterized in that the said step of finally boosting is adsorption bed finally to be boosted from the product end with product gas, or simultaneously adsorption bed is finally boosted from the product end from feed end and product gas with unstripped gas.
3,, it is characterized in that said sorbent material is at least a in zeolite molecular sieve, gac, silica gel, the activated alumina according to claim 1 or the 3 described multi-bed vacuum pressure swing adsorption process that from hydrogeneous gas mixture, extract hydrogen.
4, the multi-bed vacuum pressure swing adsorption process that from hydrogeneous gas mixture, extracts hydrogen according to claim 3, the pressure that it is characterized in that said adsorption step is 0.6～3.5MPa, the said pressure that vacuumizes step is-0.03～-0.09MPa.
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|---|---|---|---|
| CN 97107735 CN1215624A (en) | 1997-10-24 | 1997-10-24 | Multi-bed vacuum pressure swing adsorption process for extracting hydrogen from hydrogen-contg. mixed gas |
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|---|---|---|---|
| CN 97107735 CN1215624A (en) | 1997-10-24 | 1997-10-24 | Multi-bed vacuum pressure swing adsorption process for extracting hydrogen from hydrogen-contg. mixed gas |
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| CN (1) | CN1215624A (en) |
Cited By (14)
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| CN102172463A (en) * | 2011-02-28 | 2011-09-07 | 四川同盛科技有限责任公司 | Pressure swing adsorption method comprising pump-out and replacement steps |
| CN101559311B (en) * | 2009-06-02 | 2011-09-07 | 大连理工大学 | Step recovery method for centralizing refinery gas |
| CN102351147A (en) * | 2011-07-15 | 2012-02-15 | 清华大学 | Moderate temperature pressure swing adsorption method for CO2, H2S and H2 mixed gas separation |
| CN102728179A (en) * | 2012-07-17 | 2012-10-17 | 北京信诺海博石化科技发展有限公司 | Pressure-variable adsorption process for concentrating methane from low-concentration coal mine gas |
| CN103420338A (en) * | 2012-05-16 | 2013-12-04 | 中国石油化工股份有限公司 | Hydrogen gas separation method for isobutane dehydrogenation reaction gas |
| CN103664455A (en) * | 2012-09-05 | 2014-03-26 | 中国石油化工股份有限公司 | Preparation method of propylene |
| CN105879571A (en) * | 2014-12-10 | 2016-08-24 | 北京信诺海博石化科技发展有限公司 | Oil gas recycling technology for treating large amount of oil gas through adsorption method |
| CN106474924A (en) * | 2016-11-08 | 2017-03-08 | 中国工程物理研究院材料研究所 | A kind of enrichment method of trace tritium |
| CN107058863A (en) * | 2016-12-29 | 2017-08-18 | 山东钢铁股份有限公司 | A kind of 550MPa grades inexpensive steel plate for ocean engineering and its manufacture method |
| 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 |
| CN108996476A (en) * | 2018-08-21 | 2018-12-14 | 威海东兴电子有限公司 | Six tower method for producing oxygen through |
| CN110052114A (en) * | 2019-05-24 | 2019-07-26 | 成都华西化工科技股份有限公司 | A kind of vacuum pressure swing adsorption system of band backwash |
| US11344840B2 (en) | 2018-05-29 | 2022-05-31 | Sichuan Techairs Co., Ltd. | Method of purifying and recycling normal-pressure waste hydrogen by full temperature range pressure swing adsorption (FTrPSA) in manufacturing process of semiconductor |
| CN117085460A (en) * | 2022-10-11 | 2023-11-21 | 武汉城市职业学院 | Composite adsorption bed and pressure swing adsorption hydrogen production system |
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Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101559311B (en) * | 2009-06-02 | 2011-09-07 | 大连理工大学 | Step recovery method for centralizing refinery gas |
| CN102172463A (en) * | 2011-02-28 | 2011-09-07 | 四川同盛科技有限责任公司 | Pressure swing adsorption method comprising pump-out and replacement steps |
| CN102351147A (en) * | 2011-07-15 | 2012-02-15 | 清华大学 | Moderate temperature pressure swing adsorption method for CO2, H2S and H2 mixed gas separation |
| CN103420338A (en) * | 2012-05-16 | 2013-12-04 | 中国石油化工股份有限公司 | Hydrogen gas separation method for isobutane dehydrogenation reaction gas |
| CN102728179A (en) * | 2012-07-17 | 2012-10-17 | 北京信诺海博石化科技发展有限公司 | Pressure-variable adsorption process for concentrating methane from low-concentration coal mine gas |
| CN103664455B (en) * | 2012-09-05 | 2015-09-09 | 中国石油化工股份有限公司 | The preparation method of propylene |
| CN103664455A (en) * | 2012-09-05 | 2014-03-26 | 中国石油化工股份有限公司 | Preparation method of propylene |
| CN105879571A (en) * | 2014-12-10 | 2016-08-24 | 北京信诺海博石化科技发展有限公司 | Oil gas recycling technology for treating large amount of oil gas through adsorption method |
| 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 |
| CN106474924A (en) * | 2016-11-08 | 2017-03-08 | 中国工程物理研究院材料研究所 | A kind of enrichment method of trace tritium |
| CN107058863A (en) * | 2016-12-29 | 2017-08-18 | 山东钢铁股份有限公司 | A kind of 550MPa grades inexpensive steel plate for ocean engineering and its manufacture method |
| US11344840B2 (en) | 2018-05-29 | 2022-05-31 | Sichuan Techairs Co., Ltd. | Method of purifying and recycling normal-pressure waste hydrogen by full temperature range pressure swing adsorption (FTrPSA) in manufacturing process of semiconductor |
| CN108996476A (en) * | 2018-08-21 | 2018-12-14 | 威海东兴电子有限公司 | Six tower method for producing oxygen through |
| CN110052114A (en) * | 2019-05-24 | 2019-07-26 | 成都华西化工科技股份有限公司 | A kind of vacuum pressure swing adsorption system of band backwash |
| CN117085460A (en) * | 2022-10-11 | 2023-11-21 | 武汉城市职业学院 | Composite adsorption bed and pressure swing adsorption hydrogen production system |
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