CN104587797B - Method for separating and purifying CO2, CH4, CO and H2 from refining hydrogen production tail gas - Google Patents
Method for separating and purifying CO2, CH4, CO and H2 from refining hydrogen production tail gas Download PDFInfo
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- CN104587797B CN104587797B CN201410801852.0A CN201410801852A CN104587797B CN 104587797 B CN104587797 B CN 104587797B CN 201410801852 A CN201410801852 A CN 201410801852A CN 104587797 B CN104587797 B CN 104587797B
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Abstract
The invention provides a method for separating and purifying carbon dioxide, methane, carbon monoxide and hydrogen from a refining hydrogen production tail gas by adopting a five-stage pressure swing adsorption gas separation process. By adopting the method, the refining hydrogen production tail gas is fully used, a significant economic benefit can be obtained, the pollution of the refining hydrogen production tail gas to the environment is reduced, and an extremely great social benefit is obtained.
Description
Technical field
This invention relates generally to the separation of admixture of gas, specifically, relate to separating from refinery hydrogen production exhaust gas carrying
The method of pure carbon dioxide, methane, carbon monoxide and hydrogen.
Background technology
The open one of United States Patent (USP) US3564816 uses four equal pressure swing adsorption techniques of adsorbent bed secondary, for from mainly
The admixture of gas unstripped gas such as hydrogeneous and water, carbon dioxide, methane, carbon monoxide extract hydrogen.United States Patent (USP) US3986849 is public
Open a kind of employing three equal pressure swing adsorption techniques of ten adsorbent beds, for from the main hydrogen and 20.92 containing 69.22 (volume) %
The unstripped gas of the carbon dioxide of (volume) % extracts hydrogen, such as, converts from naphtha steam and gas separates hydrogen.The above-mentioned U.S. is special
Profit only extracts hydrogen from the admixture of gas unstripped gas such as the most hydrogeneous, carbon dioxide, methane and carbon monoxide, the most hydrogeneous, two
Carbon dioxide, methane and carbon monoxide contained in the admixture of gas unstripped gas such as carbonoxide, methane and carbon monoxide does not obtain
Reclaim to purifying.
Summary of the invention
The present invention provides a kind of separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas
Method.
The method of separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas of the present invention, its
Being characterised by, it is provided that five sections of pressure swing adsorption gas separation devices, order proceeds as follows:
This refinery hydrogen production exhaust gas separates dress from the first paragraph PSA Gas of these five sections of pressure swing adsorption gas separation devices
Being in bottom the first paragraph adsorption tower of adsorbed state of putting enters this and is in the first paragraph adsorption tower of adsorbed state, enters absorption
Process, the most adsorbed component carbon dioxide in this unstripped gas is adsorbed in the first paragraph adsorption tower of adsorbed state in this place,
In the middle of first paragraph not to be adsorbed, gaseous mixture flows out from this first paragraph adsorption tower top being in adsorbed state, and then this is in suction
The first paragraph adsorption tower of attached state stops adsorption process, proceeds to regenerative process, is in reproduced state, and this is easily adsorbed component dioxy
Change carbon to be desorbed, as atmospheric carbon dioxide product from being in output bottom the first paragraph adsorption tower of this reproduced state；
Gaseous mixture in the middle of this first paragraph not to be adsorbed that this first paragraph adsorption tower top being in adsorbed state is flowed out
Enter this bottom the second segment adsorption tower of adsorbed state be in adsorption-like from being in of second segment pressure swing adsorption gas separation device
In the second segment adsorption tower of state, enter adsorption process, the most adsorbed component in gaseous mixture in the middle of this first paragraph not to be adsorbed
Carbon dioxide is adsorbed in the second segment adsorption tower of adsorbed state in this place, and in the middle of second segment not to be adsorbed, gaseous mixture is from this
The second segment adsorption tower top being in adsorbed state is flowed out, and then this second segment adsorption tower being in adsorbed state stops adsorbing
Journey, proceeds to regenerative process, is in reproduced state, and this is easily adsorbed component carbon dioxide and is desorbed, and inhales as this second segment transformation
The resolution gas of attached gas fractionation unit from be in bottom the second segment adsorption tower of this reproduced state be flowed into this first paragraph transformation inhale
Reclaim in the first paragraph adsorption tower being in pressure-increasning state of attached gas fractionation unit；
Gaseous mixture in the middle of this second segment not to be adsorbed that this second segment adsorption tower top being in adsorbed state is flowed out
Enter this bottom 3rd section of adsorption tower of adsorbed state be in adsorption-like from being in of the 3rd section of pressure swing adsorption gas separation device
In 3rd section of adsorption tower of state, enter adsorption process, the most adsorbed component in gaseous mixture in the middle of this second segment not to be adsorbed
Methane is adsorbed in the 3rd section of adsorption tower of adsorbed state in this place, and in the middle of not to be adsorbed the 3rd section, gaseous mixture is in from this
3rd section of adsorption tower top of adsorbed state is flowed out, and then this 3rd section of adsorption tower being in adsorbed state stops adsorption process,
Proceeding to regenerative process, be in reproduced state, this is easily adsorbed component methane and is desorbed, as gases methane product from being in this again
Export bottom 3rd section of adsorption tower of raw state；
Gaseous mixture in the middle of this not to be adsorbed the 3rd section that this 3rd section of adsorption tower top being in adsorbed state is flowed out
Enter this bottom 4th section of adsorption tower of adsorbed state be in adsorption-like from being in of the 4th section of pressure swing adsorption gas separation device
In 4th section of adsorption tower of state, the most adsorbed component carbon monoxide entered in the middle of adsorption process, the 3rd section in gaseous mixture exists
This is adsorbed in being in the 4th section of adsorption tower of adsorbed state, and in the middle of not to be adsorbed the 4th section, gaseous mixture is in adsorption-like from this
4th section of adsorption tower top of state is flowed out, and then this 4th section of adsorption tower being in adsorbed state stops adsorption process, proceeds to again
Raw process, is in reproduced state, and this is easily adsorbed component carbon monoxide and is desorbed, as atmospheric CO product from being in this
Export bottom 4th section of adsorption tower of reproduced state；
Gaseous mixture in the middle of this not to be adsorbed the 4th section that this 4th section of adsorption tower top being in adsorbed state is flowed out
Enter this bottom 5th section of adsorption tower of adsorbed state be in adsorption-like from being in of the 5th section of pressure swing adsorption gas separation device
In 5th section of adsorption tower of state, enter adsorption process, the most adsorbed component carbon monoxide in gaseous mixture in the middle of the 4th section, two
Carbonoxide, methane, nitrogen, adsorbed in the 5th section of adsorption tower of adsorbed state in this place, hydrogen not to be adsorbed is as gas
Body hydrogen product is in the 5th section of adsorption tower top output of adsorbed state from this, then stops adsorption process, proceeds to regenerate
Journey, is in reproduced state, and this is easily adsorbed component carbon monoxide, carbon dioxide, methane, nitrogen, as the 5th section of resolution gas quilt
Resolving, the 5th section of resolution gas is out transported to this second segment transformation and inhales from being in bottom the 5th section of adsorption tower of this reproduced state
With the boosting being in the 5th section of return gas boost in the second segment adsorption tower of the purging state that is in of attached gas fractionation unit
In the second segment adsorption tower of state.
The method of separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas of the present invention, adopts
With five sections of PSA Gas separation process separating-purifying from refinery hydrogen production exhaust gas go out carbon dioxide, methane, carbon monoxide and
Hydrogen, makes refinery hydrogen production exhaust gas be fully used, and not only obtains substantial economics, and decreases refinery hydrogen production exhaust gas pair
The pollution of environment, obtains great social benefit.
Wherein, the order of this regenerative process of this first paragraph adsorption tower is :-1 displacement of 10 pressure equilibrium fall (ED)
(RP) inversely bleed off pressure-1 second segment of (BD)-1 purging (CP) for-2 times and return-10 pressure equilibrium liters of gas boost (2R)
(ER)-1 final boosting (FR).
Wherein, in this regenerative process of this first paragraph adsorption tower, inversely bleed off pressure (BD) 2 times by this, obtain purity >=
The carbon dioxide product gas of 98.5% (V).
Wherein, the order of this regenerative process of this second segment adsorption tower is: 12 times pressure equilibrium fall (ED) is inversely put for-1 time
Pressure (BD)-1 purging (CP)-1 order five sections returns-12 pressure equilibriums of gas boost (5R) and rises (ER)-1 final boosting
(FR)。
Wherein, the order of this regenerative process of the 3rd section of adsorption tower is: 11 pressure equilibrium fall (ED)-1 time is along putting
(PP)-4 displacements (RP) inversely bleed off pressure-11 the pressure equilibriums of (BD)-1 displacement boosting (R) for-2 times and rise (ER)-1 final rise
Pressure (FR).
Wherein, in this regenerative process of the 3rd section of adsorption tower, inversely bleed off pressure (BD) 2 times by this, obtain purity >=
The methane product gas of 95% (V).
Wherein, the order of this regenerative process of the 4th section of adsorption tower is: 9 pressure equilibrium fall (ED)-1 time is along putting
(PP)-5 displacements (RP) inversely bleed off pressure-9 the pressure equilibriums of (BD)-1 isolation (IR) for-2 times and rise (ER)-1 final boosting
(FR)。
Wherein, in this regenerative process of the 4th section of adsorption tower, inversely bleed off pressure (BD) 2 times by this, obtain purity >=
The carbon monoxide product gas of 97% (V).
Wherein, the order of this regenerative process of the 5th section of adsorption tower is: 4 pressure equilibrium fall (ED)-1 time is along putting
(PP) inversely bleed off pressure-4 the pressure equilibriums of (BD)-3 purgings (CP) for-1 time and rise (ER)-1 final boosting (FR).
Wherein, in this adsorption process of the 5th section of adsorption tower, obtain purity >=99.95% (V) not to be adsorbed
Hydrogen product gas.
Accompanying drawing explanation
Fig. 1 is adapted for realizing separating-purifying carbon dioxide, methane, the carbon monoxide from refinery hydrogen production exhaust gas of the present invention
Process flow diagram with five sections of pressure swing adsorption gas separation devices of the method for hydrogen.
Detailed description of the invention
Separating-purifying carbon dioxide, methane, carbon monoxide from refinery hydrogen production exhaust gas to the present invention with reference to the accompanying drawings
It is described in detail with the detailed description of the invention of the method for hydrogen, the separating-purifying titanium dioxide from refinery hydrogen production exhaust gas of the present invention
The feature and advantage of the method for carbon, methane, carbon monoxide and hydrogen will be apparent from.
Unstripped gas is refinery hydrogen production exhaust gas:
(1) component and content thereof:
(2) temperature :≤40 DEG C
(3) pressure: 0.03MPa (gauge pressure, lower same)
See Fig. 1, separating-purifying carbon dioxide, methane, carbon monoxide and the hydrogen from refinery hydrogen production exhaust gas of the present invention
Method, use five sections of pressure-variable adsorption (PSA) gas fractionation units:
First paragraph pressure-variable adsorption (PSA-1) gas fractionation unit 100, second segment pressure-variable adsorption (PSA-2) gas separate dress
Put the 300, the 4th section of pressure-variable adsorption (PSA-4) gas fractionation unit of the 200, the 3rd section of pressure-variable adsorption (PSA-3) gas fractionation unit
400 and the 5th section of pressure-variable adsorption (PSA-5) gas fractionation unit 500.
The method of separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas of the present invention, for
Five sections of pressure swing adsorption techniques:
First paragraph pressure-variable adsorption (PSA-1) technique, for adsorbing the most carbon dioxide in unstripped gas, obtains after desorbing
To CO2Content is the product gas of 98.5% (V), and in the middle of first paragraph not to be adsorbed, gaseous mixture enters second segment pressure-variable adsorption
(PSA-2) technique；The mixing in the middle of the first paragraph not to be adsorbed absorbed into of second segment pressure-variable adsorption (PSA-2) technique
Carbon dioxide in gas, the CO obtained after desorbing2Content is the mixed gas of 50% (V), and calming the anger as liter returns first paragraph change
Pressure absorption (PSA-1) technique, is recycled, and in the middle of second segment not to be adsorbed, gaseous mixture enters the 3rd section of pressure-variable adsorption
(PSA-3) technique；3rd section of pressure-variable adsorption (PSA-3) technique gaseous mixture in the middle of the second segment not to be adsorbed absorbed into
In methane, obtain CH after desorbing4Content is the product gas of 95% (V), and in the middle of not to be adsorbed the 3rd section, gaseous mixture enters
4th section of pressure-variable adsorption (PSA-4) technique；4th section of pressure-variable adsorption (PSA-4) technique for absorb into not to be adsorbed the
In the middle of three sections, the carbon monoxide in gaseous mixture, obtains the product gas that CO content is 97% (V), not to be adsorbed the 4th after desorbing
In the middle of section, gaseous mixture enters the 5th section of pressure-variable adsorption (PSA-4) technique；5th section of pressure-variable adsorption (PSA-5) technique be used for adsorbing into
Carbon monoxide in gaseous mixture, carbon dioxide, methane, nitrogen, the solution obtained after desorbing in the middle of not to be adsorbed the 4th section entered
Gassing returns to second segment pressure-variable adsorption (PSA-2) technique and calms the anger as two-stage nitration liter and purging gas, is recycled, is not inhaled
Attached for hydrogen, thus obtain H2Content is the product gas of 99.95% (V).
(1) first paragraph pressure-variable adsorption (PSA-1) gas fractionation unit 100 and first paragraph pressure-variable adsorption (PSA-1) technique:
First paragraph pressure-variable adsorption (PSA-1) gas fractionation unit 100 includes 1 first paragraph pressure-variable adsorption (PSA-1) compression
1,2 first paragraph coke filters of machine, 12,18 first paragraph adsorption tower 101-118 of 11,1 first paragraph moisture trap, 2
18,2 the first paragraph conveyings of 14,2 first paragraph displacement 15,2 first paragraph conveyance drum blower fans of heat exchanger of one section of displacement aerator are changed
Gaseous mixture surge tank 17, valve and pipeline etc. in the middle of 16,1 first paragraph of 19,1 first paragraph carbon dioxide product gas surge tank of hot device
Equipment.
First paragraph pressure-variable adsorption (PSA-1) technique, for adsorbing the most carbon dioxide in unstripped gas, obtains after desorbing
To product gas CO2, in the middle of first paragraph not to be adsorbed, gaseous mixture enters second segment pressure-variable adsorption (PSA-2) technique.
Pressure is 0.03MPa, the unstripped gas of temperature≤40 DEG C enters first paragraph pressure-variable adsorption (PSA-1) gas and separates dress
Put 100, be first pressurized to 0.85MPa by first paragraph pressure-variable adsorption (PSA-1) compressor 1, subsequently into coke filter 11, remove
Deoil hydro carbons macromolecular substances, removes aqueous water subsequently into first paragraph moisture trap 12, then enters from absorption tower bottom
It is in the adsorption tower of adsorbed state.
First paragraph pressure-variable adsorption (PSA-1) gas fractionation unit 100 is 3 adsorption tower adsorption process of 18 adsorption towers, often
Seat adsorption tower experiences successively:
1.1 absorption (A)-3.1 displacements (RP) of-2.10 pressure equilibrium fall (ED) inversely bleed off pressure (BD)-5.1-4.2 times
-6.1 second segments of secondary purging (CP) return-7.10 pressure equilibriums of gas boost (2R) and rise (ER)-8.1 final boostings
(FR)。
1.1 absorption (A): adsorption bed aluminium sesquioxide in 3 adsorption towers being in adsorbed state, silica gel
Select successively under absorption, the CO in unstripped gas2The most adsorbed component CO2It is adsorbed, mixing in the middle of first paragraph not to be adsorbed
Gas goes out from these 3 adsorption tower overhead stream, enters gaseous mixture surge tank 17 in the middle of first paragraph, presses through second segment pressure-variable adsorption (PSA-2)
Contracting machine 2 enters second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 after being forced into 2.5MPa.Biography when adsorbed material
When matter district (referred to as adsorbing forward position) arrives bed outlet reserved section initial position, turn off inlet valve and tower top at the bottom of this adsorption tower tower
Outlet valve, stops absorption.
Adsorption bed starts to proceed to regenerative process:
2.10 pressure equilibrium fall (ED): after 1 absorption (A) process terminates, along absorption direction by this adsorption tower
In tower, in the middle of the first paragraph not to be adsorbed of elevated pressures, gaseous mixture is put into other and is in 10 pressure equilibrium liter (ER) processes
The corresponding adsorption tower of lower pressure, along with in this adsorption tower tower, pressure is gradually lowered, adsorbed component CO2Constantly desorbing, solves
CO after suction2When arriving the reserved section of bed outlet, the adsorbent in the section of being reserved, cause the absorption in this adsorption tower tower
Agent all abundant CO absorption2, this process can fully reclaim the available gas not to be adsorbed of this adsorption tower bed dead space also
Improve the CO of adsorption bed2Gas concentration.
3.1 displacements (RP): after 10 pressure equilibrium fall (ED) processes terminate, highly purified product carbon dioxide gas
I.e. from the CO of first paragraph atmospheric carbon dioxide product gas surge tank 162Gas boosts to through first paragraph displacement aerator 14
0.1MPa, cools down subsequently into first paragraph displacement heat exchanger 15, then from entering adsorption bed at the bottom of this adsorption tower tower, replaces residual
Stay gaseous mixture in the middle of the first paragraph not to be adsorbed in adsorption bed, mixing in the middle of the first paragraph not to be adsorbed being displaced
Gas is vented from tower top out high point.
Inversely bleed off pressure (BD) for 4.2 times: after 1 displacement (RP) process terminates, against absorption direction by these 3 adsorption tower pressures
Power is preferably minimized, now adsorbed CO2Gas desorption out enters carbon dioxide product gas surge tank 16.More high-purity for obtaining
The regeneration of degree product carbon dioxide and beneficially adsorbent, through first paragraph conveyance drum blower fan 18 to being in the 2nd inverse put pressure condition
Tower evacuation, cools down subsequently into first paragraph delivery heat transfer device 19, then also into carbon dioxide product gas surge tank 16, obtains
98.5% (V) product gas CO2。
(1) product gas CO2Purity: >=98.5% (V)
(2) product gas CO2Pressure: >=0.01MPa
(3) product gas CO2Temperature :≤40 DEG C
5.1 purgings (CP): after (BD) process that inversely bleeds off pressure for 2 times terminates, from second segment pressure-variable adsorption (PSA-2) gas
The purge gas of the purge gas surge tank 27 of body segregation apparatus 200 enters this adsorption tower from this adsorption tower tower top, inhales this seat
Attached tower purges, further by this adsorbent CO2Out, the gas after purging is from this adsorption tower tower for gas desorption
Carbon dioxide product gas surge tank 16 is delivered at the end.
6. second segment returns gas boost (2R): after 1 purging (CP) process terminates, with from second segment pressure-variable adsorption
(PSA-2) being in of gas fractionation unit 200 inversely bleeds off pressure (BD) process analysis gas out through second segment inverse put gas buffering
Absorption direction as boosting QI rising in reverse order after tank 23 buffering this adsorption tower is boosted, reclaim second segment pressure-variable adsorption (PSA-2) gas
Being in of body segregation apparatus 200 inversely bleeds off pressure the gas that the adsorption tower of (BD) desorbs.
7.10 pressure equilibriums rise (ER): after 1 second segment return gas boost (2R) process terminates, with from other
Gaseous mixture in the middle of the first paragraph not to be adsorbed of the elevated pressures being in the adsorption tower of 10 pressure equilibrium fall (ED) processes, suitable
Absorption direction to boost this adsorption tower successively, this process is corresponding, no with 10 pressure equilibrium fall (ED) processes
It is only boost process, and the bed dead space reclaiming other adsorption tower being in 10 pressure equilibrium fall (ED) processes especially has
The process of effect gas.
8.1 final boostings (FR): after 10 pressure equilibrium liter (ER) processes terminate, be in 1 suction with from other
In the middle of the first paragraph not to be adsorbed of the adsorption tower of attached (A) process, this is in final rise against absorption direction by gaseous mixture lentamente
The adsorption column pressure of step rises to adsorptive pressure, and this adsorption tower can be made smoothly to switch to adsorb next time and reduce pressure
The fluctuation in this course of power, purity.Final boosting step is by adsorption bed pressurising to adsorptive pressure, and this adsorption tower completes
One complete " adsorption-regeneration " circulation, subsequently enters next " adsorption-regeneration " circulation.
First paragraph pressure-variable adsorption (PSA-1) technical process, time quantum see first paragraph pressure-variable adsorption (PSA-1) technique mistake
Journey, time quantum table (table 1).
First paragraph pressure-variable adsorption (PSA-1) technical process, time and pressure see first paragraph pressure-variable adsorption (PSA-1) technique
Process, time and Pressure gauge (table 2).
Whole operating process is carried out at a temperature of entering tower unstripped gas.
(2) second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 and second segment pressure-variable adsorption (PSA-2) technique:
Second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 includes 1 second segment pressure-variable adsorption (PSA-2) compression
2,17 second segment adsorption tower 201-217 of machine, 23,1 second segment purge gas surge tank 27 of 1 second segment inverse put gas surge tank,
The equipment such as valve and pipeline.
Second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 is for adsorbing from first paragraph pressure-variable adsorption (PSA-1)
Carbon dioxide in gaseous mixture in the middle of the first paragraph not to be adsorbed of gas fractionation unit 100, adsorbed carbon dioxide resolves
Out, return first paragraph pressure-variable adsorption (PSA-1) gas through second segment inverse put gas surge tank 23 with purge gas surge tank 27 to separate
Device 100, calms the anger as liter and is recycled, not inhaled of second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200
In the middle of attached second segment, gaseous mixture enters the 3rd section of pressure-variable adsorption (PSA-3) gas fractionation unit 300.
Second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 is 2 adsorption tower adsorption process of 17 adsorption towers, often
Seat adsorption tower experiences successively:
-2.12 pressure equilibrium fall (ED) of 1.1 absorption (A) inversely bleed off pressure (BD)-4.1 purging (CP)-5.1 for-3.1 times
Five sections return-6.12 pressure equilibrium liter (ER)-7.1 final boostings (FR) of gas boost (5R) one after another.
1.1 absorption (A): mixing in the middle of the first paragraph of first paragraph pressure-variable adsorption (PSA-1) gas fractionation unit 100
Gaseous mixture in the middle of the first paragraph not to be adsorbed of gas surge tank 17, pressurizes through second segment pressure-variable adsorption (PSA-2) compressor 2
From at the bottom of tower 2 that are in adsorbed state of entrance second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 after 2.50MPa
In adsorption tower, under the selection successively of adsorption bed silica gel is adsorbed, CO2Gas is adsorbed, in second segment not to be adsorbed
Between gaseous mixture flow out from these 2 adsorption tower tower tops, deliver to the 3rd section of pressure-variable adsorption (PSA-3) gas fractionation unit 300.Work as absorption
When forward position arrives bed outlet reserved section initial position, turn off inlet valve and tower top outlet valve at the bottom of this adsorption tower tower, stop inhaling
Attached.
Adsorption bed starts to proceed to regenerative process:
2.12 pressure equilibrium fall (ED): after 1 absorption (A) process terminates, along absorption direction by this adsorption tower
In tower, in the middle of the second segment not to be adsorbed of elevated pressures, gaseous mixture is put into other and is in 12 pressure equilibrium liter (ER) processes
The corresponding adsorption tower of lower pressure, along with in this adsorption tower tower, pressure is gradually lowered, adsorbed component CO2Constantly desorbing, solves
CO after suction2When arriving the reserved section of bed outlet, the adsorbent in the section of being reserved, cause the absorption in this adsorption tower tower
Agent all abundant CO absorption2, this process can fully reclaim in the middle of the second segment not to be adsorbed of these 2 adsorption tower bed dead spaces
Gaseous mixture also improves the CO of adsorption bed2Concentration.
Inversely bleed off pressure (BD) for 3.1 times: after 12 pressure equilibrium fall (ED) processes terminate, against absorption direction by this seat
Adsorption column pressure is preferably minimized, adsorbed CO2Gas desorption out, enters second segment inverse put gas surge tank 23 and carries out buffering surely
Pressure, then the second segment that is in as first paragraph pressure-variable adsorption (PSA-1) gas fractionation unit 100 returns gas boost (2R) mistake
The boosting gas of the adsorption tower of journey.
4.1 purgings (CP): after (BD) process that inversely bleeds off pressure for 1 time terminates, with from the 5th section of pressure-variable adsorption (PSA-5) gas
This adsorption tower is purged by the purge gas of the 5th section of purge gas surge tank 57 of body segregation apparatus 500 against absorption direction,
The CO further this adsorption tower adsorbed2Out, the gaseous mixture entrance second segment flowed out from this adsorption tower blows gas desorption
Scavenging surge tank 27, is then in 1 purging (CP) mistake as first paragraph pressure-variable adsorption (PSA-1) gas fractionation unit 100
The purge gas of journey delivers to the adsorption tower of first paragraph pressure-variable adsorption (PSA-1) gas fractionation unit 100.
5. the 5th section returns gas boost (5R): after 1 purging (CP) process terminates, with from the 5th section of pressure-variable adsorption
(PSA-5) the inverse put gas of the 5th section of inverse put gas surge tank 59 of gas fractionation unit 500 absorption direction as boosting QI rising in reverse order
This adsorption tower is boosted, the inverse put gas of the 5th section of pressure-variable adsorption (PSA-5) gas fractionation unit 500 is recycled.
6.12 pressure equilibriums rise (ER): after five sections of return gas boost (5R) processes of 1 order terminate, with from other
Gaseous mixture in the middle of the second segment not to be adsorbed of the elevated pressures being in the adsorption tower of 12 pressure equilibrium fall (ED) processes, along
This adsorption tower is boosted by absorption direction successively, and this process is corresponding, not only with 12 pressure equilibrium fall (ED) processes
It is boost process, and reclaims the mistake of other bed dead space available gas being in 12 pressure equilibrium fall (ED) processes especially
Journey.
7.1 final boostings (FR): after 12 pressure equilibrium liter (ER) processes terminate, in order to make this adsorption tower permissible
Smoothly switch to adsorb next time and reduce the fluctuation worked off one's feeling vent one's spleen in this course, need slowly and smoothly with from it
It is in gaseous mixture in the middle of the second segment not to be adsorbed of the adsorption tower of 1 absorption (A) process and adsorption column pressure rises to absorption
Pressure.Adsorption bed pressurising to adsorptive pressure, adsorption tower are entered the subsequent cycle cycle by final boosting (FR) step.
Second segment pressure-variable adsorption (PSA-2) technical process, time quantum see second segment pressure-variable adsorption (PSA-2) technique mistake
Journey, time quantum table (table 3).
Second segment pressure-variable adsorption (PSA-2) technical process, time and pressure see second segment pressure-variable adsorption (PSA-2) technique
Process, time and Pressure gauge (table 4).
Whole operating process is carried out at a temperature of entering tower unstripped gas.
(3) the 3rd sections of pressure-variable adsorption (PSA-3) gas fractionation units 300 and the 3rd section of pressure-variable adsorption (PSA-3) technique:
3rd section of pressure-variable adsorption (PSA-3) gas fractionation unit 300 include 21 the 3rd section of adsorption tower 301-321,2
The equipment such as three sections of aerators, 35,1 the 3rd section of methane product gas surge tank 36 of 34,2 the 3rd section of heat exchangers, valve and pipeline.
3rd section of pressure-variable adsorption (PSA-3) technique is used for adsorbing second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200
Second segment not to be adsorbed in the middle of methane in gaseous mixture, obtain product gas CH after desorbing4, gaseous mixture not to be adsorbed enters
Enter the 4th section of pressure-variable adsorption (PSA-4) technique.
3rd section of pressure-variable adsorption (PSA-3) gas fractionation unit 300 is 2 adsorption tower adsorption process of 21 adsorption towers, often
Seat adsorption tower experiences successively:
1.1 absorption (A)-2.11 pressure equilibrium fall (ED)-3.1 times are inverse along putting (PP)-4.4 displacements (RP)-5.2 times
(ER)-8.1 final boostings (FR) are risen to bleeding off pressure-7.11 the pressure equilibriums of (BD)-6.1 displacements boosting (R).
1.1 absorption (A): be in absorption (A) mistake from second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200
In the middle of the second segment not to be adsorbed of journey, gaseous mixture is from entering the 3rd section of pressure-variable adsorption (PSA-3) gas fractionation unit 300 at the bottom of tower
2 adsorption towers being in adsorbed state in, adsorption bed activated carbon selection successively adsorb under, CH4Gas is adsorbed
Getting off, in the middle of not to be adsorbed the 3rd section, gaseous mixture flows out from these 2 adsorption tower tower tops, delivers to the 4th section of pressure-variable adsorption (PSA-
4) gas fractionation unit 400.When the mass-transfer zone (referred to as adsorbing forward position) of adsorbed material arrives the reserved section initial bit of bed outlet
When putting, turn off inlet valve and tower top outlet valve at the bottom of this adsorption tower tower, stop absorption.
Adsorption bed starts to proceed to regenerative process:
2.11 pressure equilibrium fall (ED): after 1 absorption (A) process terminates, along absorption direction by this adsorption tower
In the middle of not to be adsorbed the 3rd section of interior elevated pressures, gaseous mixture is put into other and is in 11 pressure equilibrium liter (ER) processes relatively
The corresponding adsorption tower of low-pressure, along with in this adsorption tower tower, pressure is gradually lowered, adsorbed component CH4Constantly desorbing, desorbing
After CH4When arriving the reserved section of bed outlet, the adsorbent in the section of being reserved, cause the adsorbent in this adsorption tower tower
All fully adsorb CH4, this process can fully reclaim not to be adsorbed the 3rd section centre of this adsorption tower bed dead space and mix
Close gas and improve the CH of adsorption bed4Gas concentration.
3.1 times along putting (PP): after 11 pressure equilibrium fall (ED) processes terminate, along absorption direction by this adsorption tower
Interior pressure is down to about 0.10MPa.Along setting fire torch or be recycled to unstripped gas surge tank.
4.4 displacements (RP): at 1 time along letting slip after journey terminates, by the 3rd section of aerator 34 by the 3rd section of methane product
In gas surge tank 36, high-purity methane pressure-raising is to 0.12MPa, enters from the bottom of this adsorption tower after the 3rd section of heat exchanger 35 cooling
Being in the adsorption tower of replacement process, through 4 continuous displacements, the most replaced gas enters into the suction of 1 displacement boosting (R) process
Attached tower reclaims, so CH in this adsorption tower4Concentration brings up to 95%.
Inversely bleed off pressure (BD) for 5.2 times: after 4 displacement (RP) processes terminate, against absorption direction by this adsorption tower pressure
Power is preferably minimized, adsorbed CH4Gas desorption out, enters the 3rd section of methane product gas surge tank 36, obtains product gas
CH4.For obtaining the regeneration of higher purity product methane and beneficially adsorbent, through the 3rd section of aerator 34 to being in the 2nd inverse put
The adsorption tower evacuation of process, high-purity of releasing methane gas enters the 3rd section of heat exchanger 35 and cools down, and enters back into product gas buffering
Tank 36.
(1) products C H4Purity: >=95% (V)
(2) products C H4Pressure: >=0.01MPa
(3) products C H4Temperature :≤40 DEG C
6.1 displacements boosting (R): after (BD) process that inversely bleeds off pressure for 2 times terminates, with other after 4 displacement step
The displacement gas of adsorption tower is calmed the anger as the liter of 1 displacement boosting (R) step of this adsorption tower, inhales this seat along absorption direction
Attached tower carries out 1 displacement boosting (R).
7.11 pressure equilibriums rise (ER): after 1 displacement boosting (R) process terminates, be in 11 pressures with from other
Gaseous mixture in the middle of not to be adsorbed the 3rd section of power equilibrium fall (ED) process, is carried out this adsorption tower successively along absorption direction
Boosting, this process is corresponding with 11 pressure equilibrium fall (ED) processes, is not only boost process, and reclaims especially at other
Process in the bed dead space available gas of 11 pressure equilibrium fall (ED) processes.
8.1 final boostings (FR): after 11 pressure equilibrium liter (ER) processes terminate, in order to make this adsorption tower permissible
Smoothly switch to adsorb next time and reduce the fluctuation worked off one's feeling vent one's spleen in this course, need slowly and smoothly with from it
It is in gaseous mixture in the middle of not to be adsorbed the 3rd section of the adsorption tower of 1 absorption (A) process and is risen to by this adsorption column pressure
Adsorptive pressure.The steps such as final boosting are by adsorption bed pressurising to adsorptive pressure, and this adsorption tower enters the subsequent cycle cycle.
3rd section of pressure-variable adsorption (PSA-3) technical process, time quantum see the 3rd section of pressure-variable adsorption (PSA-3) technique mistake
Journey, time quantum table (table 5).
3rd section of pressure-variable adsorption (PSA-3) technical process, time and pressure see the 3rd section of pressure-variable adsorption (PSA-3) technique
Process, time and Pressure gauge (table 6).
Whole operating process is carried out at a temperature of entering tower unstripped gas.
(4) the 4th sections of pressure-variable adsorption (PSA-4) gas fractionation units 400 and the 4th section of pressure-variable adsorption (PSA-4) technique:
4th section of pressure-variable adsorption (PSA-4) gas fractionation unit 400 include 20 the 4th section of adsorption tower 401-420,2
Four sections of aerators, 45,1 the 4th section of carbon monoxide product gas surge tank 46 of 44,2 the 4th section of heat exchangers, valve and pipeline etc. set
Standby.
4th section of pressure-variable adsorption (PSA-4) gas fractionation unit 400 is for adsorbing from the 3rd section of pressure-variable adsorption (PSA-3)
In the middle of not to be adsorbed the 3rd section of gas fractionation unit 300, the carbon monoxide in gaseous mixture, obtains product gas CO after desorbing,
In the middle of not to be adsorbed the 4th section, gaseous mixture enters the 5th section of pressure-variable adsorption (PSA-5) technique.
4th section of pressure-variable adsorption (PSA-4) gas fractionation unit 400 is 2 adsorption tower adsorption process of 20 adsorption towers, often
Seat adsorption tower experiences successively:
1.1 absorption (A)-2.9 pressure equilibrium fall (ED)-3.1 times are inverse along putting (PP)-4.5 displacements (RP)-5.2 times
(ER)-8.1 final boostings (FR) are risen to bleeding off pressure-7.9 the pressure equilibriums of (BD)-6.1 isolation (IR).
1.1 absorption (A): be in absorption (A) mistake from the 3rd section of pressure-variable adsorption (PSA-3) gas fractionation unit 300
In the middle of not to be adsorbed the 3rd section of journey, gaseous mixture enters the 4th section of pressure-variable adsorption (PSA-4) gas fractionation unit from tower bottom
In 2 adsorption towers being in adsorbed state of 400, under the selection successively of adsorption bed zeolite molecular sieve is adsorbed, CO gas
Being adsorbed, in the middle of not to be adsorbed the 4th section, gaseous mixture flows out from these 2 adsorption tower tower tops, delivers to the 5th section of pressure-variable adsorption
(PSA-5) gas fractionation unit 500.At the beginning of the mass-transfer zone (referred to as adsorbing forward position) of adsorbed material arrives the reserved section of bed outlet
During beginning position, turn off inlet valve and tower top outlet valve at the bottom of this adsorption tower tower, stop absorption.
Adsorption bed starts to proceed to regenerative process:
2.9 pressure equilibrium fall (ED): after 1 absorption (A) process terminates, along absorption direction by this adsorption tower
In the middle of not to be adsorbed the 4th section of elevated pressures, gaseous mixture puts into other relatively low pressure being in 9 pressure equilibrium liter (ER) processes
The corresponding adsorption tower of power, along with in this adsorption tower tower, pressure is gradually lowered, the adsorbed continuous desorbing of component CO, the CO after desorbing
When arriving the reserved section of bed outlet, the adsorbent in the section of being reserved, cause the adsorbent in this adsorption tower tower all to fill
Dividing CO absorption, this process can fully reclaim the middle gaseous mixture of not to be adsorbed the 4th section of this adsorption tower bed dead space and carry
The CO gas concentration of high adsorption bed.
3.1 times along putting (PP): after 9 pressure equilibrium fall (ED) processes terminate, along absorption direction by this adsorption tower
Interior pressure is down to about 0.10MPa.Along setting fire torch or be recycled to unstripped gas surge tank.
4.5 displacements (RP): after terminating along (PP) process of putting at 1 time, by four sections of carbon monoxide displacement blower fans 44 by four
In section carbon monoxide product surge tank 46, high-purity carbon monooxide pressure-raising is to 0.12MPa, puts from entering to be at the bottom of these 2 adsorption towers
Changing the adsorption tower of step, through 5 continuous displacements, then displacement gas enters into the adsorption tower recovery being in boost process, so inhales
Carbonomonoxide concentration in attached tower brings up to 97%.
Inversely bleed off pressure (BD) for 5.2 times: after 5 displacement (RP) processes terminate, against absorption direction by this adsorption tower pressure
Power is preferably minimized, and adsorbed CO gas desorption out, enters the 4th section of carbon monoxide product gas surge tank 46, obtains product gas
Body CO.For obtaining the regeneration of higher purity product methane and beneficially adsorbent, through the 4th section of conveyance drum blower fan 44 to being in the 2nd time
The adsorption tower evacuation of inverse put state, high-purity of releasing methane gas enters four sections of heat exchanger coolings, enters back into product gas buffering
Tank 46.
(1) products C O purity: >=97% (V)
(2) product carbon monoxide pressure: >=0.01MPa
(3) product carbon monoxide temperature :≤40 DEG C
6.1 isolation (IR): after (BD) process that inversely bleeds off pressure for 2 times terminates, all sequencing valves are automatically switched off, and make this inhale
Attached tower and isolation of system.
7.9 pressure equilibriums rise (ER): after 1 isolation (IR) process terminates, and are in 9 pressure equilibriums with from other
Gaseous mixture in the middle of not to be adsorbed the 4th section of the elevated pressures of the adsorption tower of fall (ED) process, along absorption direction successively to this
Seat adsorption tower boosts, and this process is corresponding with 9 pressure equilibrium fall (ED) processes, is not only boost process, Er Qiegeng
It it is the mistake reclaiming other bed dead space being in 9 pressure equilibrium fall (ED) processes the 4th section of middle gaseous mixture not to be adsorbed
Journey.
8.1 final boostings (FR): after 9 pressure equilibrium liter (ER) processes terminate, in order to make this adsorption tower permissible
Smoothly switch to adsorb next time and reduce the fluctuation worked off one's feeling vent one's spleen in this course, need slowly and smoothly with from it
It is in gaseous mixture in the middle of not to be adsorbed the 4th section of the adsorption tower of 1 absorption (A) process and is risen to by this adsorption column pressure
Adsorptive pressure.The steps such as final boosting are by adsorption bed pressurising to adsorptive pressure, and this adsorption tower enters the subsequent cycle cycle.
4th section of pressure-variable adsorption (PSA-4) technical process, time quantum see the 4th section of pressure-variable adsorption (PSA-4) technique mistake
Journey, time quantum table (table 7).
4th section of pressure-variable adsorption (PSA-4) technical process, time and pressure see the 4th section of pressure-variable adsorption (PSA-4) technique
Process, time and Pressure gauge (table 8).
Whole operating process is carried out at a temperature of entering tower unstripped gas.
(5) the 5th sections of pressure-variable adsorption (PSA-5) gas fractionation units 500 and the 5th section of pressure-variable adsorption (PSA-5) technique:
5th section of pressure-variable adsorption (PSA-5) gas fractionation unit 500 include 9 the 5th section of adsorption tower 501-509,3
Five sections along venting surge tank 57,1 the 5th section of inverse put gas surge tank 59 of 53,1 the 5th section of purge gas surge tank, valve and pipeline etc.
Equipment.
5th section of pressure-variable adsorption (PSA-5) gas fractionation unit 500 is for adsorbing from the 4th section of pressure-variable adsorption (PSA-4)
Carbon monoxide in gaseous mixture in the middle of not to be adsorbed the 4th section of gas fractionation unit 400, flows out not to be adsorbed from tower top
Hydrogen, obtains product gas H2, carbon monoxide stripping gas flows out from the bottom of tower, returns second segment pressure-variable adsorption (PSA-2) gas and divides
Calm the anger as purge gas and liter from device 200, reclaimed.
5th section of pressure-variable adsorption (PSA-5) gas fractionation unit 500 is 1 adsorption tower adsorption process of 9 adsorption towers, every
Adsorption tower experiences successively:
1.1 absorption (A)-2.4 pressure equilibrium fall (ED)-3.1 times inversely bleed off pressure (BD)-5.3-4.1 times along putting (PP)
-6.4 pressure equilibriums of secondary purging (CP) rise (ER)-7.1 final boostings (FR).
1.1 absorption (A): be in absorption (A) mistake from the 4th section of pressure-variable adsorption (PSA-4) gas fractionation unit 400
In the middle of not to be adsorbed the 4th section of journey, gaseous mixture enters the 5th section of pressure-variable adsorption (PSA-5) gas fractionation unit from tower bottom
In 1 adsorption tower being in adsorbed state of 500, under the selection successively of adsorption bed is adsorbed, carbon monoxide, titanium dioxide
Carbon, methane, nitrogen are adsorbed, and hydrogen not to be adsorbed flows out from this 1 adsorption tower tower top, obtains product gas H2.When
When the mass-transfer zone (referred to as adsorbing forward position) of adsorbed material arrives bed outlet reserved section initial position, turn off this 1 adsorption tower
Inlet valve at the bottom of tower and tower top outlet valve, stop absorption.
(1) product H2Purity: >=99.95% (V)
Product H2Middle CO+CO2: ＜ 20ppm
Product H2Middle CO:＜ 10ppm
(2) product H2Pressure: >=2.400MPa
(3) product H2Temperature :≤40 DEG C
Adsorption bed starts to proceed to regenerative process:
2.4 pressure equilibrium fall (ED): after 1 absorption (A) process terminates, along absorption direction by this adsorption tower
The hydrogen not to be adsorbed of elevated pressures is put into other and is in the adsorption tower that 4 pressure equilibriums rise the lower pressure of (ER) process,
Along with in this adsorption tower tower, pressure is gradually lowered, adsorbed component carbon monoxide, carbon dioxide, methane, the continuous desorbing of nitrogen,
When carbon monoxide after desorbing, carbon dioxide, methane, nitrogen arrive bed outlet reserved section, the adsorbent in the section of being reserved is inhaled
Attached, cause the adsorbent in this 1 adsorption tower tower the most fully to adsorb, it is dead that this process can fully reclaim this 1 adsorption tower bed
The hydrogen not to be adsorbed in space.
3.1 times along putting (PP): after 4 pressure equilibrium fall (ED) processes terminate, along absorption direction in three times by this 1
Hydrogen not to be adsorbed in adsorption tower is respectively put into 3 the 5th section suitable venting surge tank 53, as the source of the gas of purging.
Inversely bleed off pressure (BD) for 4.1 times: after terminating along (PP) process of putting at 1 time, against absorption direction by this 1 adsorption tower
Pressure is preferably minimized, and adsorbed carbon monoxide, carbon dioxide, methane, nitrogen desorb, and enter the 5th section of inverse put gas and buffer
Tank 59, is then delivered to second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 as a liter pressurized air source.
5.3 purgings (CP): after (BD) process that inversely bleeds off pressure for 1 time terminates, for making adsorbent further be regenerated,
Against absorption direction, adsorption bed is purged along the hydrogen not to be adsorbed in venting surge tank 53 with 3 the 5th section respectively, enter
One step reduces carbon monoxide, carbon dioxide, methane, the dividing potential drop of nitrogen, the carbon monoxide that makes to be adsorbed, carbon dioxide, methane, nitrogen
Gas desorbing, adsorbent is regenerated again, and the carbon monoxide that desorbs, carbon dioxide, methane, nitrogen enter the 5th section of purging
Gas surge tank 57, is then delivered to second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 as source purge gas.
6.4 pressure equilibriums rise (ER): after 3 purging (CP) processes terminate, and are in 4 pressure equilibriums with from other
The hydrogen not to be adsorbed of the elevated pressures of the adsorption tower of fall (ED) process, enters this 1 adsorption tower successively along absorption direction
Row boosting, this process is corresponding with 4 pressure equilibrium fall (ED) processes, is not only boost process, and reclaims other especially
It is in the process of the bed dead space of 4 pressure equilibrium fall (ED) processes hydrogen not to be adsorbed.
7.1 final boostings (FR): after 4 pressure equilibrium liter (ER) processes terminate, in order to make this 1 adsorption tower permissible
Smoothly switch to adsorb next time and reduce the fluctuation worked off one's feeling vent one's spleen in this course, need slowly and smoothly to use product hydrogen
This 1 adsorption column pressure is risen to adsorptive pressure by gas.The steps such as final boosting by adsorption bed pressurising to adsorptive pressure, this 1
Adsorption tower enters the subsequent cycle cycle.
5th section of pressure-variable adsorption (PSA-5) technical process, time quantum see the 5th section of pressure-variable adsorption (PSA-5) technique mistake
Journey, time quantum table (table 9).
5th section of pressure-variable adsorption (PSA-5) technical process, time and pressure see the 5th section of pressure-variable adsorption (PSA-5) technique
Process, time and Pressure gauge (table 10).
Whole operating process is carried out at a temperature of entering tower unstripped gas.
Describing the present invention property and nonrestrictive description the most, it should be appreciated that
In the case of without departing from relevant scope defined by the claims, those skilled in the art can make change
And/or amendment.
Claims (10)
1. a method for separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas, its feature exists
In, it is provided that five sections of pressure swing adsorption gas separation devices, order proceeds as follows:
This refinery hydrogen production exhaust gas is from the first paragraph pressure swing adsorption gas separation device of these five sections of pressure swing adsorption gas separation devices
It is in bottom the first paragraph adsorption tower of adsorbed state and enters this and be in the first paragraph adsorption tower of adsorbed state, enter and adsorbed
Journey, the most adsorbed component carbon dioxide in this refinery hydrogen production exhaust gas is inhaled in this place in the first paragraph adsorption tower of adsorbed state
Attached, in the middle of first paragraph not to be adsorbed, gaseous mixture flows out, then at this from this first paragraph adsorption tower top being in adsorbed state
First paragraph adsorption tower in adsorbed state stops adsorption process, proceeds to regenerative process, is in reproduced state, and this is easily adsorbed component
Carbon dioxide is desorbed, as atmospheric carbon dioxide product from being in output bottom the first paragraph adsorption tower of this reproduced state；
In the middle of this first paragraph not to be adsorbed that this first paragraph adsorption tower top being in adsorbed state is flowed out, gaseous mixture is from the
Being in of two-stage nitration pressure swing adsorption gas separation device enters this bottom the second segment adsorption tower of adsorbed state and is in adsorbed state
In second segment adsorption tower, enter adsorption process, the most adsorbed component dioxy in gaseous mixture in the middle of this first paragraph not to be adsorbed
Changing carbon adsorbed in the second segment adsorption tower of adsorbed state in this place, in the middle of second segment not to be adsorbed, gaseous mixture is in from this
The second segment adsorption tower top of adsorbed state is flowed out, and then this second segment adsorption tower being in adsorbed state stops adsorption process,
Proceeding to regenerative process, be in reproduced state, this is easily adsorbed component carbon dioxide and is desorbed, as this second segment pressure-variable adsorption gas
The stripping gas of body segregation apparatus is flowed into this first paragraph pressure-variable adsorption gas from being in bottom the second segment adsorption tower of this reproduced state
Reclaim in the first paragraph adsorption tower being in pressure-increasning state of body segregation apparatus；
In the middle of this second segment not to be adsorbed that this second segment adsorption tower top being in adsorbed state is flowed out, gaseous mixture is from the
Being in of three sections of pressure swing adsorption gas separation devices enters this bottom the 3rd section of adsorption tower of adsorbed state and is in adsorbed state
In 3rd section of adsorption tower, enter adsorption process, the most adsorbed component methane in gaseous mixture in the middle of this second segment not to be adsorbed
Adsorbed in the 3rd section of adsorption tower of adsorbed state in this place, in the middle of not to be adsorbed the 3rd section, gaseous mixture is in absorption from this
3rd section of adsorption tower top of state is flowed out, and then this 3rd section of adsorption tower being in adsorbed state stops adsorption process, proceeds to
Regenerative process, is in reproduced state, and this is easily adsorbed component methane and is desorbed, as gases methane product from being in this regeneration shape
Export bottom 3rd section of adsorption tower of state；
In the middle of this not to be adsorbed the 3rd section that this 3rd section of adsorption tower top being in adsorbed state is flowed out, gaseous mixture is from the
Being in of four sections of pressure swing adsorption gas separation devices enters this bottom the 4th section of adsorption tower of adsorbed state and is in adsorbed state
In 4th section of adsorption tower, the most adsorbed component carbon monoxide entered in the middle of adsorption process, the 3rd section in gaseous mixture is in this place
Being adsorbed in the 4th section of adsorption tower of adsorbed state, in the middle of not to be adsorbed the 4th section, gaseous mixture is in adsorbed state from this
4th section of adsorption tower top is flowed out, and then this 4th section of adsorption tower being in adsorbed state stops adsorption process, proceeds to regenerate
Journey, is in reproduced state, and this is easily adsorbed component carbon monoxide and is desorbed, as atmospheric CO product from being in this regeneration
Export bottom 4th section of adsorption tower of state；
In the middle of this not to be adsorbed the 4th section that this 4th section of adsorption tower top being in adsorbed state is flowed out, gaseous mixture is from the
Being in of five sections of pressure swing adsorption gas separation devices enters this bottom the 5th section of adsorption tower of adsorbed state and is in adsorbed state
In 5th section of adsorption tower, enter the most adsorbed component carbon monoxide, titanium dioxide in gaseous mixture in the middle of adsorption process, the 4th section
Carbon, methane, nitrogen, adsorbed in the 5th section of adsorption tower of adsorbed state in this place, hydrogen not to be adsorbed is as gaseous hydrogen
Gas product is in the 5th section of adsorption tower top output of adsorbed state from this, then stops adsorption process, proceeds to regenerative process, place
In reproduced state, this is easily adsorbed component carbon monoxide, carbon dioxide, methane, nitrogen, is desorbed as the 5th section of stripping gas,
5th section of stripping gas is out transported to this second segment pressure-variable adsorption gas from being in bottom the 5th section of adsorption tower of this reproduced state
With the pressure-increasning state being in the 5th section of return gas boost in the second segment adsorption tower of the purging state that is in of body segregation apparatus
Second segment adsorption tower in.
2. according to separating-purifying carbon dioxide, methane, carbon monoxide and the hydrogen from refinery hydrogen production exhaust gas described in claim 1
Method, it is characterised in that the order of this regenerative process of this first paragraph adsorption tower is: 10 pressure equilibrium fall (ED) are put for-1 time
Change (RP) and inversely bleed off pressure-10 pressure equilibrium liters of-1 second segment return gas boost (2R) of (BD)-1 purging (CP) for-2 times
(ER)-1 final boosting (FR).
3. according to separating-purifying carbon dioxide, methane, carbon monoxide and the hydrogen from refinery hydrogen production exhaust gas described in claim 2
Method, it is characterised in that in this regenerative process of this first paragraph adsorption tower, inversely bleed off pressure (BD) 2 times by this, obtain pure
The carbon dioxide product gas of degree >=98.5% (V).
4. according to separating-purifying carbon dioxide, methane, carbon monoxide and the hydrogen from refinery hydrogen production exhaust gas described in claim 1
Method, it is characterised in that the order of this regenerative process of this second segment adsorption tower is: 12 pressure equilibrium fall (ED)-1 time is inverse
-12 pressure equilibrium liter (ER)-1 final rises of gas boost (5R) are returned to bleeding off pressure (BD)-1 purging (CP)-1 order five sections
Pressure (FR).
5. according to separating-purifying carbon dioxide, methane, carbon monoxide and the hydrogen from refinery hydrogen production exhaust gas described in claim 1
Method, it is characterised in that the order of this regenerative process of the 3rd section of adsorption tower is: 11 pressure equilibrium fall (ED)-1 time is suitable
Put (PP)-4 times displacement (RP) inversely to bleed off pressure-11 pressure equilibriums of (BD)-1 displacement boosting (R) for-2 times to rise (ER)-1 time final
Boosting (FR).
6. according to separating-purifying carbon dioxide, methane, carbon monoxide and the hydrogen from refinery hydrogen production exhaust gas described in claim 5
Method, it is characterised in that in this regenerative process of the 3rd section of adsorption tower, inversely bleed off pressure (BD) 2 times by this, obtain pure
The methane product gas of degree >=95% (V).
7. according to separating-purifying carbon dioxide, methane, carbon monoxide and the hydrogen from refinery hydrogen production exhaust gas described in claim 1
Method, it is characterised in that the order of this regenerative process of the 4th section of adsorption tower is: 9 pressure equilibrium fall (ED)-1 time is suitable
Put (PP)-5 displacements (RP) and inversely bleed off pressure-9 pressure equilibrium liter (ER)-1 the final boostings of (BD)-1 isolation (IR) for-2 times
(FR)。
8. according to separating-purifying carbon dioxide, methane, carbon monoxide and the hydrogen from refinery hydrogen production exhaust gas described in claim 7
Method, it is characterised in that in this regenerative process of the 4th section of adsorption tower, inversely bleed off pressure (BD) 2 times by this, obtain pure
The carbon monoxide product gas of degree >=97% (V).
9. according to separating-purifying carbon dioxide, methane, carbon monoxide and the hydrogen from refinery hydrogen production exhaust gas described in claim 1
Method, it is characterised in that the order of this regenerative process of the 5th section of adsorption tower is: 4 pressure equilibrium fall (ED)-1 time is suitable
Put (PP) and inversely bleed off pressure-4 pressure equilibrium liter (ER)-1 final boostings (FR) of (BD)-3 purgings (CP) for-1 time.
10. according to separating-purifying carbon dioxide, methane, carbon monoxide and the hydrogen from refinery hydrogen production exhaust gas described in claim 9
The method of gas, it is characterised in that in this adsorption process of the 5th section of adsorption tower, obtain purity not to be adsorbed >=
The hydrogen product gas of 99.95% (V).
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| US6454838B1 (en) * | 2000-06-21 | 2002-09-24 | Air Products And Chemicals, Inc. | Six bed pressure swing adsorption process with four steps of pressure equalization |
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Effective date of registration: 20191210 Address after: No. d12-10-3, north of Boyang Road, Yangpu Economic Development Zone, Hainan Province, 570000 Patentee after: Hainan Camet Gas Co., Ltd. Address before: 414012 Hunan Province, Yueyang city Yunxi District Long Chain Industrial Park Patentee before: YUEYANG CHANGLING KAIMEITE GASES CO., LTD. |
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