CN104587797A - 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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- CN104587797A CN104587797A CN201410801852.0A CN201410801852A CN104587797A CN 104587797 A CN104587797 A CN 104587797A CN 201410801852 A CN201410801852 A CN 201410801852A CN 104587797 A CN104587797 A CN 104587797A
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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
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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
The separation of relate generally to admixture of gas of the present invention, specifically, relates to the method for separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas.
Background technology
US Patent No. 3564816 is open a kind of adopts four equal pressure swing adsorption techniques of adsorbent bed secondary, for extracting hydrogen from the admixture of gas unstripped gas such as mainly hydrogeneous and water, carbon dioxide, methane, carbon monoxide.US Patent No. 3986849 open a kind of employing ten adsorbent beds three equal pressure swing adsorption techniques, extract hydrogen in unstripped gas for the carbon dioxide from main hydrogen and 20.92 (volume) % containing 69.22 (volume) %, such as, from naphtha steam reformed gas, be separated hydrogen.Above-mentioned United States Patent (USP) only extracts hydrogen from the admixture of gas unstripped gas such as mainly hydrogeneous, carbon dioxide, methane and carbon monoxide, and mainly in the admixture of gas unstripped gas such as hydrogeneous, carbon dioxide, methane and carbon monoxide, contained carbon dioxide, methane and carbon monoxide does not obtain purifying and reclaim.
Summary of the invention
The invention provides a kind of method of separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas.
The method of separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas of the present invention, is characterized in that, provides five sections of pressure swing adsorption gas separation devices, and order proceeds as follows:
This refinery hydrogen production exhaust gas enters this and is in the first paragraph adsorption tower of adsorbed state bottom the first paragraph adsorption tower being in adsorbed state of the first paragraph pressure swing adsorption gas separation device of these five sections of pressure swing adsorption gas separation devices, enter adsorption process, easy in this unstripped gas is adsorbed in the first paragraph adsorption tower that this is in adsorbed state by absorbed component carbon dioxide, do not flowed out by the first paragraph adsorption tower top that the middle gaseous mixture of first paragraph adsorbed is in adsorbed state from this, then this first paragraph adsorption tower being in adsorbed state stops adsorption process, proceed to regenerative process, be in reproduced state, this is easily desorbed by absorbed component carbon dioxide, export bottom the first paragraph adsorption tower being in this reproduced state as atmospheric carbon dioxide product,
This outflow from the first paragraph adsorption tower top that this is in adsorbed state is not entered this by gaseous mixture in the middle of the first paragraph that adsorbs and is in the second segment adsorption tower of adsorbed state bottom the second segment adsorption tower being in adsorbed state of second segment pressure swing adsorption gas separation device, enter adsorption process, this is not adsorbed by absorbed component carbon dioxide by easy in gaseous mixture in the middle of the first paragraph that adsorbs in the second segment adsorption tower that this is in adsorbed state, do not flowed out by the second segment adsorption tower top that the middle gaseous mixture of second segment adsorbed is in adsorbed state from this, then this second segment adsorption tower being in adsorbed state stops adsorption process, proceed to regenerative process, be in reproduced state, this is easily desorbed by absorbed component carbon dioxide, reclaim in the first paragraph adsorption tower being in pressure-increasning state flowing into this first paragraph pressure swing adsorption gas separation device as the resolution gas of this second segment pressure swing adsorption gas separation device bottom the second segment adsorption tower being in this reproduced state,
This outflow from the second segment adsorption tower top that this is in adsorbed state is not entered this by gaseous mixture in the middle of the second segment that adsorbs and is in the 3rd section of adsorption tower of adsorbed state bottom the 3rd section of adsorption tower being in adsorbed state of the 3rd section of pressure swing adsorption gas separation device, enter adsorption process, this is not adsorbed by absorbed component methane by easy in gaseous mixture in the middle of the second segment that adsorbs in the 3rd section of adsorption tower that this is in adsorbed state, do not flowed out by the 3rd section of adsorption tower top that the 3rd section of middle gaseous mixture adsorbed is in adsorbed state from this, then this 3rd section of adsorption tower being in adsorbed state stops adsorption process, proceed to regenerative process, be in reproduced state, this is easily desorbed by absorbed component methane, export bottom the 3rd section of adsorption tower being in this reproduced state as gases methane product,
This outflow from the 3rd section of adsorption tower top that this is in adsorbed state is not entered this by gaseous mixture in the middle of adsorb the 3rd section and is in the 4th section of adsorption tower of adsorbed state bottom the 4th section of adsorption tower being in adsorbed state of the 4th section of pressure swing adsorption gas separation device, enter adsorption process, easy in the middle of 3rd section in gaseous mixture is adsorbed in the 4th section of adsorption tower that this is in adsorbed state by absorbed component carbon monoxide, do not flowed out by the 4th section of adsorption tower top that the 4th section of middle gaseous mixture adsorbed is in adsorbed state from this, then this 4th section of adsorption tower being in adsorbed state stops adsorption process, proceed to regenerative process, be in reproduced state, this is easily desorbed by absorbed component carbon monoxide, export bottom the 4th section of adsorption tower being in this reproduced state as atmospheric CO product,
This outflow from the 4th section of adsorption tower top that this is in adsorbed state is not entered this by gaseous mixture in the middle of adsorb the 4th section and is in the 5th section of adsorption tower of adsorbed state bottom the 5th section of adsorption tower being in adsorbed state of the 5th section of pressure swing adsorption gas separation device, enter adsorption process, easy in absorbed component carbon monoxide in the middle of 4th section in gaseous mixture, carbon dioxide, methane, nitrogen, adsorbed in the 5th section of adsorption tower that this is in adsorbed state, do not exported by the 5th section of adsorption tower top that the hydrogen adsorbed is in adsorbed state as gas hydrogen product from this, then adsorption process is stopped, proceed to regenerative process, be in reproduced state, this is easily by absorbed component carbon monoxide, carbon dioxide, methane, nitrogen, be resolved as the 5th section of resolution gas, in the second segment adsorption tower that 5th section of resolution gas is out transported to the purging state that is in of this second segment pressure swing adsorption gas separation device bottom the 5th section of adsorption tower being in this reproduced state and be in and return in the second segment adsorption tower of the pressure-increasning state of gas boost with the 5th section.
The method of separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas of the present invention, five sections of PSA Gas separation process separating-purifying from refinery hydrogen production exhaust gas is adopted to go out carbon dioxide, methane, carbon monoxide and hydrogen, refinery hydrogen production exhaust gas is fully used, not only obtain substantial economics, and decrease the pollution of refinery hydrogen production exhaust gas to environment, obtain great social benefit.
Wherein, the order of this regenerative process of this first paragraph adsorption tower is: 10 isostasies are fallen (ED)-1 displacement (RP)-2 reverse (BD)-1 purging (CP)-1 second segments that bleed off pressure and returned-1 the finally boosting (FR) of gas boost (2R)-10 isostasy liters (ER).
Wherein, in this regenerative process of this first paragraph adsorption tower, reversely to be bled off pressure (BD) by these 2 times, obtain the carbon dioxide product gas of purity >=98.5% (V).
Wherein, the order of this regenerative process of this second segment adsorption tower is: 12 isostasies are fallen (ED)-1 reverse (BD)-1 purging (CP)-1 order five sections that bleeds off pressure and returned-1 the finally boosting (FR) of gas boost (5R)-12 isostasy liters (ER).
Wherein, the order of this regenerative process of the 3rd section of adsorption tower is: 11 isostasies are fallen (ED) and replaced-1 the finally boosting (FR) of boosting (R)-11 isostasy liters (ER) for-1 time along putting (PP)-4 displacements (RP)-2 reverse bleed off pressure (BD)-1 time.
Wherein, in this regenerative process of the 3rd section of adsorption tower, reversely to be bled off pressure (BD) by these 2 times, obtain the methane product gas of purity >=95% (V).
Wherein, the order of this regenerative process of the 4th section of adsorption tower is: 9 isostasies are fallen (ED) and isolated-1 the finally boosting (FR) of (IR)-9 isostasy liters (ER) for-1 time along putting (PP)-5 displacements (RP)-2 reverse bleed off pressure (BD)-1 time.
Wherein, in this regenerative process of the 4th section of adsorption tower, reversely to be bled off pressure (BD) by these 2 times, obtain the carbon monoxide product gas of purity >=97% (V).
Wherein, the order of this regenerative process of the 5th section of adsorption tower is: 4 isostasies are fallen (ED) and purged-1 the finally boosting (FR) of (CP)-4 isostasy liters (ER) for-3 times along putting (PP)-1 reverse bleed off pressure (BD)-1 time.
Wherein, in this adsorption process of the 5th section of adsorption tower, obtain not by the hydrogen product gas of purity >=99.95% (V) adsorbed.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of the five sections of pressure swing adsorption gas separation devices being suitable for the method realizing separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas of the present invention.
Detailed description of the invention
Be described in detail the detailed description of the invention of the method for separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas of the present invention with reference to the accompanying drawings, the feature and advantage of the method for separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas of the present invention will become more obvious.
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, the method for separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas of the present invention, adopts 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 fractionation unit the 200, the 3rd section of pressure-variable adsorption (PSA-3) gas fractionation unit the 300, the 4th section of pressure-variable adsorption (PSA-4) 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 is 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 CO after desorb
2content is the product gas of 98.5% (V), is not entered second segment pressure-variable adsorption (PSA-2) technique by the middle gaseous mixture of first paragraph adsorbed; Second segment pressure-variable adsorption (PSA-2) technique for adsorb enter not by the carbon dioxide in gaseous mixture in the middle of the first paragraph that adsorbs, the CO obtained after desorb
2content is the mist of 50% (V), first paragraph pressure-variable adsorption (PSA-1) technique is returned as boosting gas, recycled, do not entered the 3rd section of pressure-variable adsorption (PSA-3) technique by the middle gaseous mixture of second segment adsorbed; 3rd section of pressure-variable adsorption (PSA-3) technique for adsorb enter not by the methane in gaseous mixture in the middle of the second segment that adsorbs, obtain CH after desorb
4content is the product gas of 95% (V), is not entered the 4th section of pressure-variable adsorption (PSA-4) technique by the 3rd section of middle gaseous mixture adsorbed; 4th section of pressure-variable adsorption (PSA-4) technique for adsorb enter not by the carbon monoxide in gaseous mixture in the middle of adsorb the 3rd section, obtain the product gas that CO content is 97% (V) after desorb, do not entered the 5th section of pressure-variable adsorption (PSA-4) technique by the 4th section of middle gaseous mixture adsorbed; 5th section of pressure-variable adsorption (PSA-5) technique for adsorb enter not by carbon monoxide, carbon dioxide, methane, the nitrogen in gaseous mixture in the middle of adsorb the 4th section, the resolution gas obtained after desorb gets back to second segment pressure-variable adsorption (PSA-2) technique as two sections of boosting gas and purging gas, recycled, not by adsorb for hydrogen, thus obtain H
2content 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 comprises 1 first paragraph pressure-variable adsorption (PSA-1) compressor 1, 2 first paragraph coke filters 11, 1 first paragraph moisture trap 12, 18 first paragraph adsorption tower 101-118, 2 first paragraph displacement air blasts 14, 2 first paragraph displacement heat exchangers 15, 2 first paragraph conveyance drum blower fans 18, 2 first paragraph delivery heat transfer devices 19, 1 first paragraph carbon dioxide product gas surge tank 16, gaseous mixture surge tank 17 in the middle of 1 first paragraph, the equipment such as valve and pipeline.
First paragraph pressure-variable adsorption (PSA-1) technique, for adsorbing the most carbon dioxide in unstripped gas, obtains product gas CO after desorb
2, do not entered second segment pressure-variable adsorption (PSA-2) technique by the middle gaseous mixture of first paragraph adsorbed.
Pressure is 0.03MPa, the unstripped gas of temperature≤40 DEG C enters first paragraph pressure-variable adsorption (PSA-1) gas fractionation unit 100, first 0.85MPa is pressurized to by first paragraph pressure-variable adsorption (PSA-1) compressor 1, then coke filter 11 is entered, removing petroleum hydrocarbon class macromolecular substances, then enter first paragraph moisture trap 12 and remove aqueous water, then enter from absorption tower bottom and be in the adsorption tower of adsorbed state.
First paragraph pressure-variable adsorption (PSA-1) gas fractionation unit 100 is 18 adsorption towers, 3 absorption tower adsorbs flow processs, and every adsorption tower experiences successively:
1.1 absorption (A)-2.10 isostasies are fallen (ED)-3.1 displacements (RP)-4.2 reverse (BD)-5.1 purging (CP)-6.1 second segments that bleed off pressure and are returned-8.1 the finally boostings (FR) of gas boost (2R)-7.10 isostasy liters (ER).
1.1 absorption (A): under the adsorption bed alundum (Al2O3) in 3 adsorption towers being in adsorbed state, the adsorption selection successively of silica gel, the CO in unstripped gas
2easily by absorbed component CO
2absorbed, do not flowed out from these 3 absorption tower tops by the middle gaseous mixture of first paragraph adsorbed, enter gaseous mixture surge tank 17 in the middle of first paragraph, after second segment pressure-variable adsorption (PSA-2) compressor 2 is forced into 2.5MPa, enters second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200.When the mass-transfer zone (be called absorption forward position) of adsorbed material arrives the reserved section initial position of bed outlet, 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:
2.10 times isostasy is fallen (ED): after 1 absorption (A) process terminates, do not put into by gaseous mixture in the middle of the first paragraph that adsorbs the corresponding adsorption tower that other is in the lower pressure of 10 isostasy liter (ER) processes along absorption direction by elevated pressures in this adsorption tower tower, along with in this adsorption tower tower, pressure reduces, gradually by absorbed component CO
2continuous desorb, the CO after desorb
2when section is reserved in the outlet of arrival bed, the adsorbent in the section of being reserved, causes all abundant CO absorption of the adsorbent in this adsorption tower tower
2, what this process fully can reclaim this adsorption tower bed dead space improves the CO of adsorption bed not by the available gas that adsorbs
2gas concentration.
3.1 displacements (RP): after 10 isostasy (ED) processes of falling terminate, highly purified product carbon dioxide gas is namely from the CO of first paragraph atmospheric carbon dioxide gas product surge tank 16
2gas boosts to 0.1MPa through first paragraph displacement air blast 14, then enter first paragraph displacement heat exchanger 15 to cool, then at the bottom of this adsorption tower tower, adsorption bed is entered, displacement remain in adsorption bed not by gaseous mixture in the middle of the first paragraph that adsorbs, be displaced not by gaseous mixture in the middle of the first paragraph that adsorbs from tower top out high emptying.
4.2 times reverse bleeds off pressure (BD): after 1 displacement (RP) process terminates, drop to minimum, now by the CO adsorbed against absorption direction by these 3 adsorption column pressures
2gas desorption out enters carbon dioxide product gas surge tank 16.For obtaining more high purity product carbon dioxide and being beneficial to the regeneration of adsorbent, through first paragraph conveyance drum blower fan 18, the tower being in the 2nd inverse put pressure condition is vacuumized, then enter first paragraph delivery heat transfer device 19 to cool, then also enter carbon dioxide product gas surge tank 16, obtain 98.5% (V) product gas CO
2.
(1) product gas CO
2purity:>=98.5% (V)
(2) product gas CO
2pressure:>=0.01MPa
(3) product gas CO
2temperature :≤40 DEG C
Purge (CP) 5.1 times: reversely bleed off pressure after (BD) process terminates at 2 times, sweep gas from the sweep gas surge tank 27 of second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 enters this adsorption tower from this adsorption tower tower top, this adsorption tower is purged, further by this adsorbent CO
2out, the gas after purging delivers to carbon dioxide product gas surge tank 16 to gas desorption at the bottom of this adsorption tower tower.
6. second segment returns gas boost (2R): after 1 purging (CP) process terminates, after second segment inverse put gas surge tank 23 buffering, absorption direction to the boosting of this adsorption tower with reverse (BD) process analysis gas out that bleeds off pressure that is in from second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 as the boosting circulation of vital energy in the wrong direction, that reclaims second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 is in the gas that the reverse adsorption tower bleeding off pressure (BD) desorbs.
7.10 isostasy liters (ER): return after gas boost (2R) process terminates at 1 second segment, with be in from other 10 isostasies fall the elevated pressures of the adsorption tower of (ED) process not by gaseous mixture in the middle of the first paragraph that adsorbs, successively this adsorption tower is boosted along absorption direction, it is corresponding that (ED) process falls in this process and 10 isostasies, be not only boost process, and reclaim other especially and be in the process that the bed dead space available gas of the adsorption tower of (ED) process falls in 10 isostasies.
8.1 finally boostings (FR): after 10 isostasy liter (ER) processes terminate, with be in from other 1 absorption (A) process adsorption tower do not risen to adsorptive pressure by the adsorption column pressure that this is in most final rise step against absorption direction by gaseous mixture lentamente in the middle of the first paragraph that adsorbs, this adsorption tower can be made to switch to reposefully and to adsorb next time and reduce the fluctuation in this course of pressure, purity.Final boosting step is by adsorption bed pressurising to adsorptive pressure, and this adsorption tower completes complete " adsorption-regeneration " circulation, enters next " adsorption-regeneration " circulation subsequently.
First paragraph pressure-variable adsorption (PSA-1) technical process, time quantum are see first paragraph pressure-variable adsorption (PSA-1) technical process, time quantum table (table 1).
First paragraph pressure-variable adsorption (PSA-1) technical process, time and pressure are see first paragraph pressure-variable adsorption (PSA-1) technical process, time and Pressure gauge (table 2).
Whole operating process is entering at tower unstripped gas temperature to carry out.
(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 comprises the equipment such as 1 second segment pressure-variable adsorption (PSA-2) compressor, 2,17 second segment adsorption tower 201-217,1 second segment inverse put gas surge tank 23,1 second segment sweep gas surge tank 27, valve and pipeline.
Second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 for absorption from first paragraph pressure-variable adsorption (PSA-1) gas fractionation unit 100 not by the carbon dioxide in gaseous mixture in the middle of the first paragraph that adsorbs, parsed by the carbon dioxide adsorbed, first paragraph pressure-variable adsorption (PSA-1) gas fractionation unit 100 is returned through second segment inverse put gas surge tank 23 and sweep gas surge tank 27, recycled as boosting gas, second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 do not entered the 3rd section of pressure-variable adsorption (PSA-3) gas fractionation unit 300 by gaseous mixture in the middle of the second segment that adsorbs.
Second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 is 17 adsorption towers, 2 absorption tower adsorbs flow processs, and every adsorption tower experiences successively:
1.1 absorption (A)-2.12 isostasies are fallen (ED)-3.1 reverse (BD)-4.1 purgings (CP)-5.1 order five sections that bleed off pressure and are returned-7.1 the finally boostings (FR) of gas boost (5R)-6.12 isostasy liters (ER).
1.1 absorption (A): from gaseous mixture surge tank 17 in the middle of the first paragraph of first paragraph pressure-variable adsorption (PSA-1) gas fractionation unit 100 not by gaseous mixture in the middle of the first paragraph that adsorbs, what after second segment pressure-variable adsorption (PSA-2) compressor 2 pressurizes 2.50MPa, enter second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 at the bottom of tower is in 2 adsorption towers of adsorbed state, under the adsorption selection successively of adsorption bed silica gel, CO
2gas is absorbed, and is not flowed out from these 2 adsorption tower tower tops by the middle gaseous mixture of second segment adsorbed, delivers to the 3rd section of pressure-variable adsorption (PSA-3) gas fractionation unit 300.When adsorbing the outlet of forward position arrival bed and reserving section initial 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:
2.12 times isostasy is fallen (ED): after 1 absorption (A) process terminates, do not put into by gaseous mixture in the middle of the second segment that adsorbs the corresponding adsorption tower that other is in the lower pressure of 12 isostasy liter (ER) processes along absorption direction by elevated pressures in this adsorption tower tower, along with in this adsorption tower tower, pressure reduces, gradually by absorbed component CO
2continuous desorb, the CO after desorb
2when section is reserved in the outlet of arrival bed, the adsorbent in the section of being reserved, causes all abundant CO absorption of the adsorbent in this adsorption tower tower
2, what this process fully can reclaim these 2 adsorption tower bed dead spaces improves the CO of adsorption bed not by gaseous mixture in the middle of the second segment that adsorbs
2concentration.
3.1 times reverse bleeds off pressure (BD): after 12 isostasy (ED) processes of falling terminate, and drops to minimum, by the CO adsorbed against absorption direction by this adsorption column pressure
2gas desorption out, enter second segment inverse put gas surge tank 23 and carry out buffering voltage stabilizing, be in then as first paragraph pressure-variable adsorption (PSA-1) gas fractionation unit 100 the boosting gas that second segment returns the adsorption tower of gas boost (2R) process.
Purge (CP) 4.1 times: reversely bleed off pressure after (BD) process terminates at 1 time, this adsorption tower is purged, further by the CO of this absorption tower adsorbs against absorption direction by the sweep gas of the 5th section of sweep gas surge tank 57 from the 5th section of pressure-variable adsorption (PSA-5) gas fractionation unit 500
2gas desorption out, the gaseous mixture flowed out from this adsorption tower enters second segment sweep gas surge tank 27, then delivers to the adsorption tower of first paragraph pressure-variable adsorption (PSA-1) gas fractionation unit 100 as the sweep gas being in 1 purging (CP) process 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, absorption direction to the boosting of this adsorption tower with the inverse put gas of the 5th section of inverse put gas surge tank 59 from the 5th section of pressure-variable adsorption (PSA-5) gas fractionation unit 500 as the boosting circulation of vital energy in the wrong direction, the inverse put gas of the 5th section of pressure-variable adsorption (PSA-5) gas fractionation unit 500 is recycled.
6.12 isostasy liters (ER): return after gas boost (5R) process terminates 1 order five sections, with be in from other 12 isostasies fall the elevated pressures of the adsorption tower of (ED) process not by gaseous mixture in the middle of the second segment that adsorbs, successively this adsorption tower is boosted along absorption direction, it is corresponding that (ED) process falls in this process and 12 isostasies, be not only boost process, and reclaim other especially and be in the process that the bed dead space available gas of (ED) process falls in 12 isostasies.
7.1 finally boostings (FR): after 12 isostasy liter (ER) processes terminate, can switch to reposefully to make this adsorption tower and adsorb next time and reduce the fluctuation of working off one's feeling vent one's spleen in this course, need slowly and reposefully be in from other 1 absorption (A) process adsorption tower not by adsorb second segment centre gaseous mixture adsorption column pressure is risen to adsorptive pressure.Final boosting (FR) step is by adsorption bed pressurising to adsorptive pressure, and adsorption tower enters next cycle period.
Second segment pressure-variable adsorption (PSA-2) technical process, time quantum are see second segment pressure-variable adsorption (PSA-2) technical process, time quantum table (table 3).
Second segment pressure-variable adsorption (PSA-2) technical process, time and pressure are see second segment pressure-variable adsorption (PSA-2) technical process, time and Pressure gauge (table 4).
Whole operating process is entering at tower unstripped gas temperature to carry out.
(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 comprises the equipment such as 21 the 3rd section of adsorption tower 301-321,2 the 3rd section of air blasts, 34,2 the 3rd section of heat exchangers 35,1 the 3rd section of methane product gas surge tank 36, valve and pipeline.
3rd section of pressure-variable adsorption (PSA-3) technique for adsorb second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 not by the methane in gaseous mixture in the middle of the second segment that adsorbs, obtain product gas CH after desorb
4, do not entered the 4th section of pressure-variable adsorption (PSA-4) technique by the gaseous mixture adsorbed.
3rd section of pressure-variable adsorption (PSA-3) gas fractionation unit 300 is 21 adsorption towers, 2 absorption tower adsorbs flow processs, and every adsorption tower experiences successively:
1.1 absorption (A)-2.11 isostasies are fallen (ED) and are replaced-8.1 the finally boostings (FR) of boosting (R)-7.11 isostasy liters (ER) for-6.1 times along putting (PP)-4.4 displacements (RP)-5.2 reverse bleed off pressure (BD)-3.1 times.
1.1 absorption (A): from second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 absorption (A) process that is at the bottom of tower, do not entered the 3rd section of pressure-variable adsorption (PSA-3) gas fractionation unit 300 by the second segment centre gaseous mixture adsorbed be in 2 adsorption towers of adsorbed state, under the adsorption selection successively of adsorption bed activated carbon, CH
4gas is absorbed, and is not flowed out from these 2 adsorption tower tower tops by the 3rd section of middle gaseous mixture adsorbed, delivers to the 4th section of pressure-variable adsorption (PSA-4) gas fractionation unit 400.When the mass-transfer zone (be called absorption forward position) of adsorbed material arrives the reserved section initial position of bed outlet, 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 times isostasy is fallen (ED): after 1 absorption (A) process terminates, along absorption direction by elevated pressures in this adsorption tower not by adsorb the 3rd section in the middle of gaseous mixture put into the corresponding adsorption tower that other is in the lower pressure of 11 isostasy liter (ER) processes, along with in this adsorption tower tower, pressure reduces, gradually by absorbed component CH
4continuous desorb, the CH after desorb
4when section is reserved in the outlet of arrival bed, the adsorbent in the section of being reserved, causes the adsorbent in this adsorption tower tower all fully to adsorb CH
4, what this process fully can reclaim this adsorption tower bed dead space improves the CH of adsorption bed not by gaseous mixture in the middle of adsorb the 3rd section
4gas concentration.
3.1 times along putting (PP): after 11 isostasy (ED) processes of falling terminate, along adsorbing direction by Pressure Drop in this adsorption tower 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 air blast 34 by high-purity methane pressure-raising in the 3rd section of methane product gas surge tank 36 to 0.12MPa, at the bottom of this adsorption tower, the adsorption tower being in replacement process is entered after the 3rd section of heat exchanger 35 cools, through 4 displacements continuously, then replaced gas enters into the adsorption tower recovery of 1 displacement boosting (R) process, the CH like this in this adsorption tower
4concentration brings up to 95%.
5.2 times reverse bleeds off pressure (BD): after 4 displacement (RP) processes terminate, drop to minimum, by the CH adsorbed against absorption direction by this adsorption column pressure
4gas desorption out, enters the 3rd section of methane product gas surge tank 36, obtains product gas CH
4.For obtaining more high purity product methane and being beneficial to the regeneration of adsorbent, vacuumize the adsorption tower being in the 2nd inverse put process through the 3rd section of air blast 34, high-purity of releasing methane gas enters the 3rd section of heat exchanger 35 and cools, then enters gas product surge tank 36.
(1) products C H
4purity:>=95% (V)
(2) products C H
4pressure:>=0.01MPa
(3) products C H
4temperature :≤40 DEG C
6.1 displacements boosting (R): reversely bleed off pressure after (BD) process terminates at 2 times, with the displacement gas of other adsorption tower after 4 displacement step as the boosting gas of 1 displacement boosting (R) step of this adsorption tower, along absorption direction, 1 displacement boosting (R) is carried out to this adsorption tower.
7.11 isostasy liters (ER): after 1 displacement boosting (R) process terminates, with be in from other 11 isostasies fall (ED) process not by gaseous mixture in the middle of adsorb the 3rd section, successively this adsorption tower is boosted along absorption direction, it is corresponding that (ED) process falls in this process and 11 isostasies, be not only boost process, and reclaim other especially and be in the process that the bed dead space available gas of (ED) process falls in 11 isostasies.
8.1 finally boostings (FR): after 11 isostasy liter (ER) processes terminate, can switch to reposefully to make this adsorption tower and adsorb next time and reduce the fluctuation of working off one's feeling vent one's spleen in this course, need slowly and reposefully be in from other 1 absorption (A) process adsorption tower by adsorb the 3rd section centre gaseous mixture, this adsorption column pressure is not risen to adsorptive pressure.The steps such as final boosting are by adsorption bed pressurising to adsorptive pressure, and this adsorption tower enters next cycle period.
3rd section of pressure-variable adsorption (PSA-3) technical process, time quantum are see the 3rd section of pressure-variable adsorption (PSA-3) technical process, time quantum table (table 5).
3rd section of pressure-variable adsorption (PSA-3) technical process, time and pressure are see the 3rd section of pressure-variable adsorption (PSA-3) technical process, time and Pressure gauge (table 6).
Whole operating process is entering at tower unstripped gas temperature to carry out.
(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 comprises the equipment such as 20 the 4th section of adsorption tower 401-420,2 the 4th section of air blasts, 44,2 the 4th section of heat exchangers 45,1 the 4th section of carbon monoxide product gas surge tank 46, valve and pipeline.
4th section of pressure-variable adsorption (PSA-4) gas fractionation unit 400 for absorption from the 3rd section of pressure-variable adsorption (PSA-3) gas fractionation unit 300 not by the carbon monoxide in gaseous mixture in the middle of adsorb the 3rd section, obtain product gas CO after desorb, do not entered the 5th section of pressure-variable adsorption (PSA-5) technique by the 4th section of middle gaseous mixture adsorbed.
4th section of pressure-variable adsorption (PSA-4) gas fractionation unit 400 is 20 adsorption towers, 2 absorption tower adsorbs flow processs, and every adsorption tower experiences successively:
1.1 absorption (A)-2.9 isostasies are fallen (ED) and are isolated-8.1 the finally boostings (FR) of (IR)-7.9 isostasy liters (ER) for-6.1 times along putting (PP)-4.5 displacements (RP)-5.2 reverse bleed off pressure (BD)-3.1 times.
1.1 absorption (A): from the 3rd section of pressure-variable adsorption (PSA-3) gas fractionation unit 300 absorption (A) process that is in do not entered the 4th section of pressure-variable adsorption (PSA-4) gas fractionation unit 400 by adsorb the 3rd section centre gaseous mixture from tower bottom be in 2 adsorption towers of adsorbed state, under the adsorption selection successively of adsorption bed zeolite molecular sieve, CO gas is absorbed, do not flowed out from these 2 adsorption tower tower tops by the 4th section of middle gaseous mixture adsorbed, deliver to the 5th section of pressure-variable adsorption (PSA-5) gas fractionation unit 500.When the mass-transfer zone (be called absorption forward position) of adsorbed material arrives the reserved section initial position of bed outlet, 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 times isostasy is fallen (ED): after 1 absorption (A) process terminates, along absorption direction by elevated pressures in this adsorption tower not by adsorb the 4th section in the middle of gaseous mixture put into the corresponding adsorption tower that other is in the lower pressure of 9 isostasy liter (ER) processes, along with in this adsorption tower tower, pressure reduces gradually, by the continuous desorb of absorbed component CO, when section is reserved in CO arrival bed outlet after desorb, adsorbent in the section of being reserved, cause all abundant CO absorption of the adsorbent in this adsorption tower tower, what this process fully can reclaim this adsorption tower bed dead space improves the CO gas concentration of adsorption bed not by gaseous mixture in the middle of adsorb the 4th section.
3.1 times along putting (PP): after 9 isostasy (ED) processes of falling terminate, along adsorbing direction by Pressure Drop in this adsorption tower 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, blower fans 44 are replaced by high-purity carbon monooxide pressure-raising in four sections of carbon monoxide product surge tanks 46 to 0.12MPa by four sections of carbon monoxide, the adsorption tower being in displacement step is entered at the bottom of these 2 adsorption towers, through 5 displacements continuously, then displacement gas enters into the adsorption tower recovery being in boost process, and the carbonomonoxide concentration in such adsorption tower brings up to 97%.
5.2 times reverse bleeds off pressure (BD): after 5 displacement (RP) processes terminate, against absorption direction, this adsorption column pressure is dropped to minimum, by the CO gas desorption that adsorbs out, enter the 4th section of carbon monoxide product gas surge tank 46, obtain product gas CO.For obtaining more high purity product methane and being beneficial to the regeneration of adsorbent, vacuumize the adsorption tower being in the 2nd inverse put state through the 4th section of conveyance drum blower fan 44, high-purity of releasing methane gas enters four sections of heat exchangers coolings, then enters gas product surge 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): reversely bleed off pressure after (BD) process terminates at 2 times, all sequencing valves cut out automatically, make this adsorption tower and isolation of system.
7.9 isostasy liters (ER): after 1 isolation (IR) process terminates, with be in from other 9 isostasies fall the elevated pressures of the adsorption tower of (ED) process not by gaseous mixture in the middle of adsorb the 4th section, successively this adsorption tower is boosted along absorption direction, it is corresponding that (ED) process falls in this process and 9 isostasies, be not only boost process, and reclaim other especially and be in bed dead space that (ED) process falls in 9 isostasies not by the process of gaseous mixture in the middle of adsorb the 4th section.
8.1 finally boostings (FR): after 9 isostasy liter (ER) processes terminate, can switch to reposefully to make this adsorption tower and adsorb next time and reduce the fluctuation of working off one's feeling vent one's spleen in this course, need slowly and reposefully be in from other 1 absorption (A) process adsorption tower by adsorb the 4th section centre gaseous mixture, this adsorption column pressure is not risen to adsorptive pressure.The steps such as final boosting are by adsorption bed pressurising to adsorptive pressure, and this adsorption tower enters next cycle period.
4th section of pressure-variable adsorption (PSA-4) technical process, time quantum are see the 4th section of pressure-variable adsorption (PSA-4) technical process, time quantum table (table 7).
4th section of pressure-variable adsorption (PSA-4) technical process, time and pressure are see the 4th section of pressure-variable adsorption (PSA-4) technical process, time and Pressure gauge (table 8).
Whole operating process is entering at tower unstripped gas temperature to carry out.
(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 comprises the equipment such as 9 the 5th section of adsorption tower 501-509,3 the 5th section suitable venting surge tank 53,1 the 5th section of sweep gas surge tank 57,1 the 5th section of inverse put gas surge tank 59, valve and pipeline.
5th section of pressure-variable adsorption (PSA-5) gas fractionation unit 500 for absorption from the 4th section of pressure-variable adsorption (PSA-4) gas fractionation unit 400 not by the carbon monoxide in gaseous mixture in the middle of adsorb the 4th section, flow out not by the hydrogen adsorbed from tower top, obtain product gas H
2, carbon monoxide stripping gas goes out from tower bottom flow, returns second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 as sweep gas and boosting gas, is reclaimed.
5th section of pressure-variable adsorption (PSA-5) gas fractionation unit 500 is 9 adsorption towers, 1 absorption tower adsorbs flow process, and every adsorption tower experiences successively:
1.1 absorption (A)-2.4 isostasies are fallen (ED) and are purged-7.1 the finally boostings (FR) of (CP)-6.4 isostasy liters (ER) for-5.3 times along putting (PP)-4.1 reverse bleed off pressure (BD)-3.1 times.
1.1 absorption (A): from the 4th section of pressure-variable adsorption (PSA-4) gas fractionation unit 400 absorption (A) process that is in do not entered the 5th section of pressure-variable adsorption (PSA-5) gas fractionation unit 500 by adsorb the 4th section centre gaseous mixture from tower bottom be in 1 adsorption tower of adsorbed state, under the adsorption selection successively of adsorption bed, carbon monoxide, carbon dioxide, methane, nitrogen are absorbed, do not flowed out from this 1 adsorption tower tower top by the hydrogen adsorbed, obtain product gas H
2.When the mass-transfer zone (be called absorption forward position) of adsorbed material arrives the reserved section initial position of bed outlet, turn off inlet valve and tower top outlet valve at the bottom of this 1 adsorption tower tower, stop absorption.
(1) product H
2purity:>=99.95% (V)
Product H
2middle CO+CO
2: < 20ppm
Product H
2middle CO:< 10ppm
(2) product H
2pressure:>=2.400MPa
(3) product H
2temperature :≤40 DEG C
Adsorption bed starts to proceed to regenerative process:
2.4 times isostasy is fallen (ED): after 1 absorption (A) process terminates, along absorption direction elevated pressures in this adsorption tower do not put into by the hydrogen adsorbed the adsorption tower that other is in the lower pressure of 4 isostasy liter (ER) processes, along with in this adsorption tower tower, pressure reduces gradually, by absorbed component carbon monoxide, carbon dioxide, methane, the continuous desorb of nitrogen, carbon monoxide after desorb, carbon dioxide, methane, when section is reserved in the outlet of nitrogen arrival bed, adsorbent in the section of being reserved, the adsorbent in this 1 adsorption tower tower is caused all fully to adsorb, this process can fully reclaim this 1 adsorption tower bed dead space not by the hydrogen adsorbed.
3.1 times along putting (PP): after 4 isostasy (ED) processes of falling terminate, along absorption direction divide three times by this 1 adsorption tower not by the hydrogen adsorbed put into respectively 3 the 5th section along venting surge tank 53, as purge source of the gas.
4.1 times reverse bleeds off pressure (BD): after terminating along (PP) process of putting at 1 time, against absorption direction, this 1 adsorption column pressure is dropped to minimum, desorbed by the carbon monoxide, carbon dioxide, methane, the nitrogen that adsorb, enter the 5th section of inverse put gas surge tank 59, then deliver to second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 as boosting source of the gas.
Purge (CP) 5.3 times: reversely bleed off pressure after (BD) process terminates at 1 time, further regenerated for making adsorbent, respectively with not purged adsorption bed against absorption direction by the hydrogen adsorbed in 3 the 5th section suitable venting surge tank 53, further reduction carbon monoxide, carbon dioxide, methane, the dividing potential drop of nitrogen, make by the carbon monoxide adsorbed, carbon dioxide, methane, nitrogen desorb, adsorbent is regenerated again, the carbon monoxide desorbed, carbon dioxide, methane, nitrogen enters the 5th section of sweep gas surge tank 57, then second segment pressure-variable adsorption (PSA-2) gas fractionation unit 200 is delivered to as source purge gas.
6.4 isostasy liters (ER): after 3 purging (CP) processes terminate, with be in from other 4 isostasies fall the elevated pressures of the adsorption tower of (ED) process not by the hydrogen adsorbed, successively this 1 adsorption tower is boosted along absorption direction, it is corresponding that (ED) process falls in this process and 4 isostasies, be not only boost process, and reclaim other especially and be in bed dead space that (ED) process falls in 4 isostasies not by the process of hydrogen of adsorbing.
7.1 finally boostings (FR): after 4 isostasy liter (ER) processes terminate, adsorb next time to make this 1 adsorption tower switch to reposefully and reduce the fluctuation of working off one's feeling vent one's spleen in this course, needing slowly and reposefully with product hydrogen, this 1 adsorption column pressure to be risen to adsorptive pressure.The steps such as final boosting are by adsorption bed pressurising to adsorptive pressure, and this 1 adsorption tower enters next cycle period.
5th section of pressure-variable adsorption (PSA-5) technical process, time quantum are see the 5th section of pressure-variable adsorption (PSA-5) technical process, time quantum table (table 9).
5th section of pressure-variable adsorption (PSA-5) technical process, time and pressure are see the 5th section of pressure-variable adsorption (PSA-5) technical process, time and Pressure gauge (table 10).
Whole operating process is entering at tower unstripped gas temperature to carry out.
Describing the present invention property and nonrestrictive description according to the embodiment of the present invention, but should be understood that when not departing from relevant scope defined by the claims, those skilled in the art can make and changing and/or amendment.
Claims (10)
1. the method for separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas, is characterized in that, provide five sections of pressure swing adsorption gas separation devices, and order proceeds as follows:
This refinery hydrogen production exhaust gas enters this and is in the first paragraph adsorption tower of adsorbed state bottom the first paragraph adsorption tower being in adsorbed state of the first paragraph pressure swing adsorption gas separation device of these five sections of pressure swing adsorption gas separation devices, enter adsorption process, easy in this unstripped gas is adsorbed in the first paragraph adsorption tower that this is in adsorbed state by absorbed component carbon dioxide, do not flowed out by the first paragraph adsorption tower top that the middle gaseous mixture of first paragraph adsorbed is in adsorbed state from this, then this first paragraph adsorption tower being in adsorbed state stops adsorption process, proceed to regenerative process, be in reproduced state, this is easily desorbed by absorbed component carbon dioxide, export bottom the first paragraph adsorption tower being in this reproduced state as atmospheric carbon dioxide product,
This outflow from the first paragraph adsorption tower top that this is in adsorbed state is not entered this by gaseous mixture in the middle of the first paragraph that adsorbs and is in the second segment adsorption tower of adsorbed state bottom the second segment adsorption tower being in adsorbed state of second segment pressure swing adsorption gas separation device, enter adsorption process, this is not adsorbed by absorbed component carbon dioxide by easy in gaseous mixture in the middle of the first paragraph that adsorbs in the second segment adsorption tower that this is in adsorbed state, do not flowed out by the second segment adsorption tower top that the middle gaseous mixture of second segment adsorbed is in adsorbed state from this, then this second segment adsorption tower being in adsorbed state stops adsorption process, proceed to regenerative process, be in reproduced state, this is easily desorbed by absorbed component carbon dioxide, reclaim in the first paragraph adsorption tower being in pressure-increasning state flowing into this first paragraph pressure swing adsorption gas separation device as the resolution gas of this second segment pressure swing adsorption gas separation device bottom the second segment adsorption tower being in this reproduced state,
This outflow from the second segment adsorption tower top that this is in adsorbed state is not entered this by gaseous mixture in the middle of the second segment that adsorbs and is in the 3rd section of adsorption tower of adsorbed state bottom the 3rd section of adsorption tower being in adsorbed state of the 3rd section of pressure swing adsorption gas separation device, enter adsorption process, this is not adsorbed by absorbed component methane by easy in gaseous mixture in the middle of the second segment that adsorbs in the 3rd section of adsorption tower that this is in adsorbed state, do not flowed out by the 3rd section of adsorption tower top that the 3rd section of middle gaseous mixture adsorbed is in adsorbed state from this, then this 3rd section of adsorption tower being in adsorbed state stops adsorption process, proceed to regenerative process, be in reproduced state, this is easily desorbed by absorbed component methane, export bottom the 3rd section of adsorption tower being in this reproduced state as gases methane product,
This outflow from the 3rd section of adsorption tower top that this is in adsorbed state is not entered this by gaseous mixture in the middle of adsorb the 3rd section and is in the 4th section of adsorption tower of adsorbed state bottom the 4th section of adsorption tower being in adsorbed state of the 4th section of pressure swing adsorption gas separation device, enter adsorption process, easy in the middle of 3rd section in gaseous mixture is adsorbed in the 4th section of adsorption tower that this is in adsorbed state by absorbed component carbon monoxide, do not flowed out by the 4th section of adsorption tower top that the 4th section of middle gaseous mixture adsorbed is in adsorbed state from this, then this 4th section of adsorption tower being in adsorbed state stops adsorption process, proceed to regenerative process, be in reproduced state, this is easily desorbed by absorbed component carbon monoxide, export bottom the 4th section of adsorption tower being in this reproduced state as atmospheric CO product,
This outflow from the 4th section of adsorption tower top that this is in adsorbed state is not entered this by gaseous mixture in the middle of adsorb the 4th section and is in the 5th section of adsorption tower of adsorbed state bottom the 5th section of adsorption tower being in adsorbed state of the 5th section of pressure swing adsorption gas separation device, enter adsorption process, easy in absorbed component carbon monoxide in the middle of 4th section in gaseous mixture, carbon dioxide, methane, nitrogen, adsorbed in the 5th section of adsorption tower that this is in adsorbed state, do not exported by the 5th section of adsorption tower top that the hydrogen adsorbed is in adsorbed state as gas hydrogen product from this, then adsorption process is stopped, proceed to regenerative process, be in reproduced state, this is easily by absorbed component carbon monoxide, carbon dioxide, methane, nitrogen, be resolved as the 5th section of resolution gas, in the second segment adsorption tower that 5th section of resolution gas is out transported to the purging state that is in of this second segment pressure swing adsorption gas separation device bottom the 5th section of adsorption tower being in this reproduced state and be in and return in the second segment adsorption tower of the pressure-increasning state of gas boost with the 5th section.
2. according to the method for separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas according to claim 1, it is characterized in that, the order of this regenerative process of this first paragraph adsorption tower is: 10 isostasies are fallen (ED)-1 displacement (RP)-2 reverse (BD)-1 purging (CP)-1 second segments that bleed off pressure and returned-1 the finally boosting (FR) of gas boost (2R)-10 isostasy liters (ER).
3. according to the method for separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas according to claim 2, it is characterized in that, in this regenerative process of this first paragraph adsorption tower, reversely to be bled off pressure (BD) by these 2 times, obtain the carbon dioxide product gas of purity >=98.5% (V).
4. according to the method for separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas according to claim 1, it is characterized in that, the order of this regenerative process of this second segment adsorption tower is: 12 isostasies are fallen (ED)-1 reverse (BD)-1 purging (CP)-1 order five sections that bleeds off pressure and returned-1 the finally boosting (FR) of gas boost (5R)-12 isostasy liters (ER).
5. according to the method for separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas according to claim 1, it is characterized in that, the order of this regenerative process of the 3rd section of adsorption tower is: 11 isostasies are fallen (ED) and replaced-1 the finally boosting (FR) of boosting (R)-11 isostasy liters (ER) for-1 time along putting (PP)-4 displacements (RP)-2 reverse bleed off pressure (BD)-1 time.
6. according to the method for separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas according to claim 5, it is characterized in that, in this regenerative process of the 3rd section of adsorption tower, reversely to be bled off pressure (BD) by these 2 times, obtain the methane product gas of purity >=95% (V).
7. according to the method for separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas according to claim 1, it is characterized in that, the order of this regenerative process of the 4th section of adsorption tower is: 9 isostasies are fallen (ED) and isolated-1 the finally boosting (FR) of (IR)-9 isostasy liters (ER) for-1 time along putting (PP)-5 displacements (RP)-2 reverse bleed off pressure (BD)-1 time.
8. according to the method for separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas according to claim 7, it is characterized in that, in this regenerative process of the 4th section of adsorption tower, reversely to be bled off pressure (BD) by these 2 times, obtain the carbon monoxide product gas of purity >=97% (V).
9. according to the method for separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas according to claim 1, it is characterized in that, the order of this regenerative process of the 5th section of adsorption tower is: 4 isostasies are fallen (ED) and purged-1 the finally boosting (FR) of (CP)-4 isostasy liters (ER) for-3 times along putting (PP)-1 reverse bleed off pressure (BD)-1 time.
10. according to the method for separating-purifying carbon dioxide, methane, carbon monoxide and hydrogen from refinery hydrogen production exhaust gas according to claim 9, it is characterized in that, in this adsorption process of the 5th section of adsorption tower, obtain not by the hydrogen product gas of purity >=99.95% (V) adsorbed.
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| CN105802686A (en) * | 2016-03-08 | 2016-07-27 | 安庆凯美特气体有限公司 | Method for extracting liquefied gas and pentane from refinery tail gas |
| CN107376603A (en) * | 2017-08-03 | 2017-11-24 | 中石化炼化工程（集团）股份有限公司 | Remove CO in hydrogen manufacturing conversion gas pressure swing adsorption technique tail gas2Method |
| CN114849425A (en) * | 2022-04-13 | 2022-08-05 | 辽宁石油化工大学 | Equipment and method for separating and enriching carbon dioxide in flue gas |
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