CN1273374C - Technology of combined extreacting carbon dioxide and hydrogen using medium varying gas decarbonization-varying pressure adsorption - Google Patents
Technology of combined extreacting carbon dioxide and hydrogen using medium varying gas decarbonization-varying pressure adsorption Download PDFInfo
- Publication number
- CN1273374C CN1273374C CNB2004100568088A CN200410056808A CN1273374C CN 1273374 C CN1273374 C CN 1273374C CN B2004100568088 A CNB2004100568088 A CN B2004100568088A CN 200410056808 A CN200410056808 A CN 200410056808A CN 1273374 C CN1273374 C CN 1273374C
- Authority
- CN
- China
- Prior art keywords
- gas
- hydrogen
- tower
- pressure
- absorption
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- 239000007789 gas Substances 0.000 title claims abstract description 65
- 239000001257 hydrogen Substances 0.000 title claims abstract description 34
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 34
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 32
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 29
- 238000001179 sorption measurement Methods 0.000 title abstract description 13
- 238000005516 engineering process Methods 0.000 title abstract description 12
- 229910002092 carbon dioxide Inorganic materials 0.000 title abstract description 8
- 239000001569 carbon dioxide Substances 0.000 title abstract description 5
- 238000000034 method Methods 0.000 claims abstract description 42
- 238000003795 desorption Methods 0.000 claims abstract description 18
- 238000006243 chemical reaction Methods 0.000 claims abstract description 11
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 5
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 5
- 238000010521 absorption reaction Methods 0.000 claims description 38
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 16
- 235000011089 carbon dioxide Nutrition 0.000 claims description 13
- 230000008859 change Effects 0.000 claims description 13
- 230000009466 transformation Effects 0.000 claims description 12
- 239000002594 sorbent Substances 0.000 claims description 11
- 239000012535 impurity Substances 0.000 claims description 9
- 230000000274 adsorptive effect Effects 0.000 claims description 6
- 238000005261 decarburization Methods 0.000 claims description 6
- 238000005406 washing Methods 0.000 claims description 6
- 230000006837 decompression Effects 0.000 claims description 5
- 150000002431 hydrogen Chemical class 0.000 claims description 5
- 238000007670 refining Methods 0.000 claims description 5
- 230000008929 regeneration Effects 0.000 claims description 5
- 238000011069 regeneration method Methods 0.000 claims description 5
- 239000004215 Carbon black (E152) Substances 0.000 claims description 3
- 239000002156 adsorbate Substances 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 230000000994 depressogenic effect Effects 0.000 claims description 3
- 239000000446 fuel Substances 0.000 claims description 3
- 239000002250 absorbent Substances 0.000 claims description 2
- 230000002745 absorbent Effects 0.000 claims description 2
- 230000002411 adverse Effects 0.000 claims description 2
- 238000011084 recovery Methods 0.000 abstract description 10
- 238000005262 decarbonization Methods 0.000 abstract description 4
- 230000006835 compression Effects 0.000 abstract 1
- 238000007906 compression Methods 0.000 abstract 1
- 230000003247 decreasing effect Effects 0.000 abstract 1
- 230000008569 process Effects 0.000 description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 11
- 239000000047 product Substances 0.000 description 7
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 description 4
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 description 4
- 239000000284 extract Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000007701 flash-distillation Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000002808 molecular sieve Substances 0.000 description 3
- 238000010926 purge Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 3
- 239000004261 Ascorbyl stearate Substances 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 239000011692 calcium ascorbate Substances 0.000 description 2
- 235000009508 confectionery Nutrition 0.000 description 2
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000000542 fatty acid esters of ascorbic acid Substances 0.000 description 2
- 238000011010 flushing procedure Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000000541 tocopherol-rich extract Substances 0.000 description 2
- 239000010457 zeolite Substances 0.000 description 2
- YZCKVEUIGOORGS-OUBTZVSYSA-N Deuterium Chemical compound [2H] YZCKVEUIGOORGS-OUBTZVSYSA-N 0.000 description 1
- 241000948268 Meda Species 0.000 description 1
- 241000931197 Themeda Species 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000003973 irrigation Methods 0.000 description 1
- 230000002262 irrigation Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 239000006210 lotion Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 238000007747 plating Methods 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000004080 punching Methods 0.000 description 1
- 239000012264 purified product Substances 0.000 description 1
- 239000004172 quinoline yellow Substances 0.000 description 1
- 230000007420 reactivation Effects 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000012958 reprocessing Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000012163 sequencing technique Methods 0.000 description 1
- PPASLZSBLFJQEF-RKJRWTFHSA-M sodium ascorbate Substances [Na+].OC[C@@H](O)[C@H]1OC(=O)C(O)=C1[O-] PPASLZSBLFJQEF-RKJRWTFHSA-M 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 239000002076 α-tocopherol Substances 0.000 description 1
Landscapes
- Separation Of Gases By Adsorption (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The present invention relates to combined technology for extracting hydrogen and carbon dioxide in intermediate conversion gas produced by a steam converting method of dry gas hydrocarbons by series connection of wet decarbonization and pressure swing adsorption. The technology of the present invention can obtain high purity hydrogen and carbon dioxide; when used, the combined technology enhances the hydrogen recovery rate and increases the desorption tower pressure through decreasing the CO2 recovery rate to increase the CO2 pressure and to decrease the compression cost of CO2 recovery.
Description
Technical field
The present invention relates to be a kind of be raw material hydrocarbon producing dry gas, petroleum naphtha etc. with lighter hydrocarbons, Sweet natural gas, refinery exhaust, secondary processing---separating hydrogen gas and carbonic acid gas in the change gas steam reforming is produced in, adopt wet method decarburization series connection transformation adsorption combined method that the component of conversion gas is carried out separation processes, can obtain highly purified hydrogen and purity greater than 98% carbonic acid gas, this method is particularly suitable for doing raw material hydrogen manufacturing with refinery's secondary processing tail gas, wherein becomes gas N
2The content height.This specialty belongs to the refining of petroleum field, its key problem in technology:
Adopt wet method decarburization and transformation absorption (PSA) serial connection technology.Pass through optimization of process conditions.At the suitable CO that reduces
2Under the condition of the rate of recovery, promptly improved the hydrogen receipts, can improve again and separate gassing (98%CO
2) pressure, reduced the production cost of follow-up CO 2 refining system.
Background technology
Be used for becoming the gas hydrogen purification device and be divided into two big classes: wet method and dry method.The main in the past wet method that adopts of eighties of last century the eighties, benzene Fei Erfa and MDEA method are that it represents flow process in the wet method; Its advantage is a hydrogen rate of recovery height, can obtain high purity byproduct CO
2, but product purity is not high, in needing, low conversion methanation handles.After the eighties, along with transformation absorption PSA development of technology, device maximizes and makes progress, and becomes gas during PSA separates and obtains the high-purity hydrogen technology and worldwide refine oil hydrogenation unit and obtained widespread use.It is low that PSA has a running cost, the operational stability height, the advantage that product purity is high, but the hydrogen rate of recovery of PSA device low be the common problem that operating PSA runs into.CN1248482A has invented a kind of from conversion gas separation of hydrogen, nitrogen and pure CO
2Pressure swing absorption process.US3,751,878 have introduced the PSA system of low-quality Sweet natural gas with zeolite molecular sieve selective adsorption carbonic acid gas, operating system is under 1000psia pressure and 300 ℃, this system as irrigation, deviates from methane that zeolite top is adsorbed and the methane in the purge column internal pore with carbonic acid gas.US4,077,779 has introduced the application of carbonaceous molecular sieve selective adsorption separating carbon dioxide and hydrogen or methane.After adsorption step, with CO 2 high pressure flushing, step-down then and deviate from carbonic acid gas, then in depress with extraneous gas such as air purge.Then again this tower is vacuumized, deviate from extraneous gas and residual carbon dioxide.US4,915,711 have recorded and narrated a kind of pressure swing absorption process, and this method is produced two kinds of highly purified products, adopts product (methane) and this sorbent material of regenerating under the vacuum condition of approximate 1-4psia in secondary product (carbonic acid gas) the low-pressure washing tower.This method is included in the emptying process pressure balanced optional step between tower.US5,026,406th, US4, the improved a little extension of 915,711 methods part.CN1349841A has invented a kind of the separation with the transformation suction type by the methanol synthesizing process off-gas and has produced high-purity hydrogen and CO
2Method.Extract CO with PSA
2, obtain the CO of desorb
2Pressure is low, has increased CO
2Cost squeeze.Along with the rising of crude oil price, how to improve device for producing hydrogen H
2The rate of recovery and CO
2Utilization ratio, reduce the developing direction that its comprehensive energy consumption, cost have become this field WeiLai Technology simultaneously.
Summary of the invention
The present invention adopts wet method decarbonization process series connection transformation absorption (PSA) new combination process, promptly uses chemical absorption method (wet method) to remove the middle CO that becomes in the gas
2, can be used for production food grade and technical grade CO
2Purified gas advances PSA device purification H
2, because density of hydrogen improves in the purified gas, to compare with simple employing PSA process unit, the hydrogen rate of recovery that can improve total system has the better economic prospect more than 5%.Promptly improve hydrogen and receive, can reach the purpose of exhaust gas utilization again.
In addition, because the refinery extracts CO from device for producing hydrogen
2, adopt the method for wet method decarburization to reclaim CO
2, its rate of recovery is less demanding, and this invention is to utilize to increase desorption tower pressure, and few CO slows down
2The rate of recovery realizes reducing CO
2Cost squeeze reaches the purpose of maximizing the benefits.
Description of drawings
Fig. 1 is the process frame chart of middle change air humidity method decarburization series connection transformation absorption (PSA) combination process.
Among the figure: A. absorption tower B. is cold change 1 C. separatory, 1 D.PSA E. flash distillation F. desorption tower G. cold change 2 H. washing I. separatory, 2 J. carbonic acid gas already cold 3 L. that change of the section of system K. boost
Fig. 2 is the middle air humidity method decarbonization process schema that becomes described in the embodiment 1.
Among the figure: 1. become gas air cooling A-101 9. separator Z-102 10. reflux pump P-301/1 among the reboiler E-303 2. regenerator column T-302 3. air cooler E-3014. aftercooler E-302 5.V-301 6.V-3027. behind the change gas boiler water preheater among the separator Z-1038., 211. lean pump P-302/1,2 12. semi-leanpump P-303/1,2 13.E-30414.E-305,15. absorption tower T-301,16. purified gas water cooler E-30717.V-303 18.V-304,19. separator Z-104,20. water cooler E-10421. storage tank V-304,22. cold E-306
Embodiment
The present invention is achieved in that pressure is that 0.3～3Mpa, temperature are 40～70 ℃, CO
2Content fully contacts with the absorbent solution from desorption tower (the being lean solution) adverse current of temperature into 40～60 ℃ in absorption tower (A) at 11%～20% middle change gas, has absorbed CO in the middle change gas
2Rich solution, draw and deliver to desorb workshop section at (A) end from the absorption tower, at pressure is to go earlier flash tank (E) flash distillation under 0.03～0.5Mpa condition, its flashed vapour is sent to the low pressure gas pipe network, it is that 0.03～0.5Mpa, temperature are 100～120 ℃ and carry out desorb, the high-purity CO that comes out in desorption tower (F) top from flash tank (E) bottom at pressure that the rich solution that flashes off gases such as dissolved hydrogen, methane in addition enters desorption tower (F)
2Gas enters CO behind overcooling water cooler (G) washing, skimmer (G) separatory
2Refining workshop section.The lean solution of coming out from desorption tower (F) bottom is cooled to 40～60 ℃ through water cooler (K) and boosts to 0.3～3Mpa again and deliver to top, absorption tower (A); CO
2Content cools off again through the laggard PSA of skimmer (C) separatory (D) through water cooler (B) at 0.1%～10% purified gas, utilize sorbent material that adsorbate is depressed its adsorptive capacity difference at the difference branch, under the adsorptive pressure of 0.5～3.0MPa, to the impurity in the purified gas adsorb selectively and High Purity Hydrogen and bring out from product and to enter pure hydrogen pipe network after coming.Obtain regeneration after having adsorbed these impurity of sorbent material decompression desorption of impurity, the gas that desorption goes out enters system low-voltage gas pipe network and makes fuel and use.
The PSA sorbent material is the composition of 4A, 5A molecular sieve, gac, Kiselgel A, activated alumina etc., has supplier to provide.
PSA adopts " 933 " technology, i.e. nine towers operation, the air inlet simultaneously of three towers are adsorbed, all pressed for three times.(40 ℃ of purified gass, 1.0～3.0Mpa) enter native system, by inlet end from bottom to up by being in each adsorption bed of adsorption step, system operation can require to finish switching to each sequencing valve by the computer control follow procedure, the loop cycle of each adsorption bed is identical, and a plurality of tower combinations can reach the purpose of continuous separating hydrogen gas.Each tower all will experience absorption, drop pressure, secondary drop pressure, three equal pressure drops, forward put pressure, reverse pressure, flushing, three boost pressures, secondary boost pressure, boost pressure, the final punching press of product totally ten one steps of putting in primary sorption, reprocessing cycle.
Other each adsorption towers are all wanted corresponding above-mentioned 11 steps of finishing, and just stagger on the time, thereby whole pressure swing adsorption system form a continuous operational process.
Pressure swing adsorption decarbonization is to utilize sorbent material (CO, CO
2Special-purpose sorbent material) to CO and CO
2Loading capacity change with the variation of pressure, adsorb CO and CO in the thick hydrogen during pressurization
2, decompression vacuum pumping makes its desorb, makes sorbent material obtain regeneration.Thereby remove CO and CO in the thick hydrogen
2The exchange of two towers is carried out.Need to prove that the absorption of PSA transformation has belonged to prior art.
O is taken off in catalysis
2Be with the take off O of thick hydrogen by the catalyzer of packing into (activated alumina plating palladium)
2Tower, the trace oxygen in the thick hydrogen generates water with H-H reaction chemical combination under the effect of catalyzer, remove the O in the dehydrogenation
2, reach the purpose of purification.Reaction equation is as follows:
Embodiment 1 (is that example describes with accompanying drawing 2)
Dry gas with catalytic cracking unit is a raw material, adopts the conversion gas (forming as table 1) of hydrocarbon, one section reforming hydrogen manufacturing explained hereafter of steam to carry out the wet method decarburization, and technical process is seen in the accompanying drawing 2.
Becoming gas in the table-1 forms
| Form | H 2 | CO 2 | CO | CH 4 | N 2 | H 2O | □ |
| V％ | 73.5 | 13.5 | 1.O | 4.0 | 8.0 | Saturated | 100 |
Becoming gas is to enter bottom, absorption tower in the absorption section (T301) under 40 ℃ of conditions at pressure into 1.35Mpa, temperature behind pressure 1.4Mpa, 150 ℃ of reboilers (E-303) through regenerator column of temperature, separator (Z103), air cooler A-101, separator Z-102, water cooler E104, knockout drum (Z104) separatory, pass through the absorption tower from bottom to top, in Ta Nei and the semi lean solution and the lean solution counter current contact in succession of stream from top to down, the MDEA solution (lean solution) under 40 ℃ of conditions after the holomorphosis is from CO
2Top, absorption tower enters, and passes through the absorption tower from top to bottom; 70 ℃ of MDEA solution (semi lean solution) after the incomplete regen-eration are from CO
2The middle part, absorption tower enters, from top to bottom by absorption tower T301; The MEDA solution of countercurrent flow fully contacts in the absorption tower with conversion gas, and most of carbonic acid gas is absorbed and enters liquid phase, unabsorbed H in the conversion gas
2, CH
4, CO, N
2Draw from the top, absorption tower etc. component, through purified gas water cooler E-307, enter separator V303, go out the separator purified gas and be sent to transformation absorption and put forward the hydrogen operation, purified gas is formed and is seen Table-2.
Table-2
Absorb CO
2MEDA solution claim rich solution, (T301) bottom extracts from the absorption tower, arrive first flash tank V304, flash distillation under 0.3Mpa pressure, it is online that flashed vapour is delivered to transformation absorption PSA parsing tracheae, flash tank outlet at bottom MEDA rich solution, arrives two sections regenerator column T302 epimere tower tops and is decompressed under 0.03Mpa, 70 ℃ of conditions and resolves the hot regenerated CO of tower under the while quilt through semi lean solution and rich solution interchanger E305 lean solution and rich solution interchanger E304 by its level control valve
2, H
2The hot vapour counter current contact of O stripping, the flashed vapour composition sees Table-2.
About 80% of semi lean solution, going up the pars infrasegmentalis intercepting basin from regenerator column (T302) draws, by semi-leanpump (P303/1,2) extract out, after semi lean solution and rich solution interchanger E305 heat exchange cooling, enter absorption tower T-301 middle part, about 20% semi lean solution continue regenerator column hypomere (stripping stage) from top to bottom with hot gas flow (CO
2, H
2O) counter current contact, hot reactivation, reboiler temperature are 108 ℃, the regenerated thermal source provides (heating agent is 150 ℃ of left and right sides low temperature shift gas) by tower bottom reboiler E303.
Regenerator column T302 hypomere outlet at bottom holomorphosis solution (lean solution) is extracted out by lean pump (P302/1,2), arrives top, absorption tower do absorption lean solution through lean solution and rich solution interchanger E304, lean solution water cooler E306 Liquid level adjusting valve.
CO
2Regenerator column T302 epimere top exit gas enters resurgent gases washing separator V301 through resurgent gases air cooler E301, water cooler E302, with washing lotion to CO
2Air purge is washed, and removes the MDEA solution of deentrainment, washes back liquid stream and reinstates reflux pump (P301/1,2) extraction with phlegma one, delivers to CO
2Trim the top of column liquid is made at regenerator column epimere top, and clean carbonic acid gas can enter hypomere operation or refining through voltage-controlled valve.Clean carbonic acid gas composition sees Table-3.
Purified gas advances PSA.Utilize sorbent material that adsorbate is depressed its adsorptive capacity difference at the difference branch, under the adsorptive pressure of 0.5～3.0MPa, to the impurity in the purified gas adsorb selectively and High Purity Hydrogen and bring out from product and to enter pure hydrogen pipe network after coming.H2 〉=96%. hydrogen yields 93% obtains regeneration after having adsorbed these impurity of sorbent material decompression desorption of impurity, and the gas that desorption goes out enters system low-voltage gas pipe network and makes fuel and use.
Embodiment 2 is increased to 0.15Mpa with regenerator column T302 epimere tower top desorption pressures, promptly improves and reclaims CO
2Pressure experiment, other condition is identical with embodiment 1, and purified gas, flashed vapour and stripping gas (carbonic acid gas) are formed as table 3.
Table-3
Claims (2)
1, a kind of combined method that adopts the absorption of wet method decarburization series connection transformation, the product that this method is produced from dry gas hydrocarbon steam conversion method is again by separating hydrogen gas and carbonic acid gas in the change gas the gained of medium voltage transformation device reaction back, it is characterized in that: middle change gas is that lean solution fully contacts with the absorbent solution of adverse current in the absorption tower, has absorbed CO in the middle change gas
2Solution to be rich solution draw at the bottom of the absorption tower delivers to desorb workshop section, remove earlier flash tank, its flashed vapour is sent to the low pressure gas pipe network, the rich solution that flashes off dissolved hydrogen, methane and other gas in addition removes CO
2The top decompression desorb of desorption tower, and the hot regenerated CO of tower under the while quilt
2, H
2O hot steam stripping, CO
2The high-purity CO that comes out in the desorption tower top
2Gas enters CO behind overcooling washing, separatory
2Refining workshop section; The lean solution of coming out from the desorption tower bottom is through cooling off, boosting and deliver to the top, absorption tower; The middle gas of gas after the absorption tower absorbs that becomes is that purified gas enters PSA transformation absorption workshop section; Utilize sorbent material that adsorbate is depressed its adsorptive capacity difference at the difference branch, under the adsorptive pressure of 0.5～3.0MPa, to the impurity in the purified gas adsorb selectively and High Purity Hydrogen and bring out from product and to enter pure hydrogen pipe network after coming; Obtain regeneration after having adsorbed these impurity of sorbent material decompression desorption of impurity, the gas that desorption goes out enters system low-voltage gas pipe network and makes fuel and use.
2, method according to claim 1, absorption tower pressure wherein is 0.3～3MPa, desorption tower pressure is 0.03～0.5MPa, CO in the purified gas on absorption tower
2Content is at 0.1%～10% (V).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100568088A CN1273374C (en) | 2004-08-20 | 2004-08-20 | Technology of combined extreacting carbon dioxide and hydrogen using medium varying gas decarbonization-varying pressure adsorption |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100568088A CN1273374C (en) | 2004-08-20 | 2004-08-20 | Technology of combined extreacting carbon dioxide and hydrogen using medium varying gas decarbonization-varying pressure adsorption |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1618729A CN1618729A (en) | 2005-05-25 |
| CN1273374C true CN1273374C (en) | 2006-09-06 |
Family
ID=34764251
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2004100568088A Expired - Lifetime CN1273374C (en) | 2004-08-20 | 2004-08-20 | Technology of combined extreacting carbon dioxide and hydrogen using medium varying gas decarbonization-varying pressure adsorption |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1273374C (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100358797C (en) * | 2006-07-12 | 2008-01-02 | 宋三奎 | Method and apparatus for recovering flash evaporated gas from decarbonizing synthetic ammonia |
| DE102007056625B3 (en) * | 2007-11-23 | 2008-09-04 | Lurgi Gmbh | Method for treating a process gas stream containing carbon dioxide during the production of pure synthesis gas from crude comprises compressing contaminated carbon dioxide and removing the impurities by stripping |
| CN102502632B (en) * | 2011-10-18 | 2014-04-16 | 中国华能集团清洁能源技术研究院有限公司 | Carbon dioxide purification system integrated with synthesis gas desulfurization system |
| CN102397739B (en) * | 2011-11-11 | 2012-12-26 | 南通正拓气体有限公司 | Technology for preparing hydrogen and carbon dioxide by purifying and refining biological butanol fermentation tail gas and purification plant thereof |
| CN102659104B (en) * | 2012-05-08 | 2014-04-09 | 中国石油化工股份有限公司 | Process for extracting carbon dioxide and hydrogen jointly by decarburization-pressure swing adsorption of shift gas |
| CN102642832B (en) * | 2012-05-08 | 2014-08-20 | 中国石油化工股份有限公司 | Combined process for extracting carbon dioxide and hydrogen from middle pressure transformed gas through decarburization-washing-PSA (pressure swing adsorption) |
| CN102659105B (en) * | 2012-05-08 | 2014-04-09 | 中国石油化工股份有限公司 | Technology for extracting carbon dioxide and hydrogen by combining medium temperature shift gas decarbonization-stationary bed-pressure swing adsorption |
| CN114712984B (en) * | 2022-03-16 | 2023-03-03 | 四川天采科技有限责任公司 | Substitution process for recycling CO2 through full-temperature-range pressure swing adsorption for amine absorption decarburization in natural gas SMB hydrogen production |
| CN118543224A (en) * | 2024-07-25 | 2024-08-27 | 东莞新能源研究院 | Low-energy-consumption combined carbon trapping method |
-
2004
- 2004-08-20 CN CNB2004100568088A patent/CN1273374C/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| CN1618729A (en) | 2005-05-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8192527B2 (en) | Purification method by hydrogen adsorbtion with cogeneration of CO2 stream pressure | |
| US8746009B2 (en) | Production of hydrogen from a reforming gas and simultaneous capture of CO2 co-product | |
| CN102659104B (en) | Process for extracting carbon dioxide and hydrogen jointly by decarburization-pressure swing adsorption of shift gas | |
| CN104891439A (en) | Method for increasing of recovery rate of hydrogen from reformed gas | |
| CN1273374C (en) | Technology of combined extreacting carbon dioxide and hydrogen using medium varying gas decarbonization-varying pressure adsorption | |
| CN109294645A (en) | It is a kind of to utilize coke-stove gas synthesis of methanol with joint production LNG, richness H2Device and method | |
| CN107778124B (en) | Full-temperature range adsorption extraction separation method for recovering H2 and C2+ from refinery dry gas | |
| CN102659105B (en) | Technology for extracting carbon dioxide and hydrogen by combining medium temperature shift gas decarbonization-stationary bed-pressure swing adsorption | |
| CN110228792B (en) | Deep decarburization process for synthesis gas | |
| CN104031681A (en) | Method for recovering ethylene and hydrogen from refinery dry gases by combining cold oil absorption and pressure swing adsorption (PSA) | |
| CN104986735A (en) | Method for improving hydrogen recovery rate | |
| CN104059692A (en) | Method for recovering hydrogen, C2 and fraction light dydrocarbon in combination manner | |
| CN104043315A (en) | Method for recovering hydrogen and ethylene from high and low pressure refinery dry gas | |
| CN101530718A (en) | Process for adsorbing and separating light hydrocarbon in F-T synthesis circulation gas by variable temperature and pressure | |
| CN209052640U (en) | It is a kind of to utilize coke-stove gas synthesis of methanol with joint production LNG, richness H2Device | |
| CN111548824A (en) | Combined process for recovering and separating refinery dry gas | |
| CN216604669U (en) | Device for recovering high-purity hydrogen by utilizing styrene dehydrogenation tail gas | |
| CN114712984B (en) | Substitution process for recycling CO2 through full-temperature-range pressure swing adsorption for amine absorption decarburization in natural gas SMB hydrogen production | |
| CN102642832B (en) | Combined process for extracting carbon dioxide and hydrogen from middle pressure transformed gas through decarburization-washing-PSA (pressure swing adsorption) | |
| CN112374959B (en) | Method for separating ethylene and ethane in catalytic dry gas | |
| CN1069687C (en) | Process for purification to obtain high-purity synthetic gas by adsorption | |
| CN112521245A (en) | Method for producing high-purity ethylene | |
| CN114955996A (en) | Hydrogen energy recovery and purification device in natural gas liquefaction process | |
| CN114917723A (en) | CO recovery from flue gas 2 Full temperature range pressure swing adsorption process | |
| CN210645772U (en) | Produce acid gas purifier of multiple purity hydrogen sulfide |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20060906 |