CN1069708A - Pressure swing adsorption process for removing carbon dioxide from ammonia plant shift gas - Google Patents
Pressure swing adsorption process for removing carbon dioxide from ammonia plant shift gas Download PDFInfo
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- CN1069708A CN1069708A CN91107278A CN91107278A CN1069708A CN 1069708 A CN1069708 A CN 1069708A CN 91107278 A CN91107278 A CN 91107278A CN 91107278 A CN91107278 A CN 91107278A CN 1069708 A CN1069708 A CN 1069708A
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- 238000000034 method Methods 0.000 title claims abstract description 47
- 238000001179 sorption measurement Methods 0.000 title claims abstract description 41
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 28
- 230000008569 process Effects 0.000 title claims abstract description 25
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 22
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title abstract description 42
- 229910002092 carbon dioxide Inorganic materials 0.000 title abstract description 4
- 239000001569 carbon dioxide Substances 0.000 title abstract description 4
- 235000011089 carbon dioxide Nutrition 0.000 claims description 20
- 238000010521 absorption reaction Methods 0.000 claims description 16
- 238000002955 isolation Methods 0.000 claims description 6
- 230000000274 adsorptive effect Effects 0.000 claims description 5
- 239000002994 raw material Substances 0.000 claims description 4
- 230000009466 transformation Effects 0.000 claims description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 239000000741 silica gel Substances 0.000 claims description 3
- 229910002027 silica gel Inorganic materials 0.000 claims description 3
- 239000002594 sorbent Substances 0.000 claims description 3
- 229910021536 Zeolite Inorganic materials 0.000 claims description 2
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 2
- 239000002808 molecular sieve Substances 0.000 claims description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 2
- 239000010457 zeolite Substances 0.000 claims description 2
- -1 gac Chemical compound 0.000 claims 1
- 239000007789 gas Substances 0.000 abstract description 57
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 48
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 24
- 239000001257 hydrogen Substances 0.000 abstract description 21
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 21
- 238000006243 chemical reaction Methods 0.000 abstract description 18
- 238000011084 recovery Methods 0.000 abstract description 14
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 10
- 238000005261 decarburization Methods 0.000 abstract description 4
- 239000007788 liquid Substances 0.000 abstract description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 18
- 238000005516 engineering process Methods 0.000 description 14
- 239000012535 impurity Substances 0.000 description 12
- 150000002431 hydrogen Chemical class 0.000 description 11
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 description 6
- 238000005262 decarbonization Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- 239000003463 adsorbent Substances 0.000 description 3
- 235000012538 ammonium bicarbonate Nutrition 0.000 description 3
- 229910052786 argon Inorganic materials 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 235000009508 confectionery Nutrition 0.000 description 3
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 2
- JJEJDZONIFQNHG-UHFFFAOYSA-N [C+4].N Chemical compound [C+4].N JJEJDZONIFQNHG-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000003763 carbonization Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 229910052802 copper Inorganic materials 0.000 description 2
- 239000010949 copper Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229940072033 potash Drugs 0.000 description 1
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Substances [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 1
- 235000015320 potassium carbonate Nutrition 0.000 description 1
- RUOJZAUFBMNUDX-UHFFFAOYSA-N propylene carbonate Chemical compound CC1COC(=O)O1 RUOJZAUFBMNUDX-UHFFFAOYSA-N 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/042—Purification by adsorption on solids
- C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention provides a pressure swing adsorption method for removing carbon dioxide from synthetic ammonia conversion gas. It features that multiple-bed vacuum pressure-varying adsorption technique is used, and each bed is sequentially subjected to adsorption, pressure-equalizing drop, reverse pressure-reducing, vacuumizing, pressure-equalizing rise and final pressure-increasing steps in a cycle. The invention also has the characteristics of simple flow, convenient operation, no pollution liquid generated in the decarburization process, no more than 0.5 percent (molar volume) of carbon dioxide in the purified gas, more than 95 percent and 90 percent of hydrogen and nitrogen recovery rate of the purified gas respectively, obvious energy saving and consumption reduction, and the like.
Description
The method with transformation absorption (hereinafter to be referred as PSA) of the invention relates to removes carbonic acid gas from hydrogeneous and mixed gas nitrogen in the conversion gas of particularly ammonia synthesis process.
From gases such as synthetic gas, Sweet natural gas, town gas, remove the carbonic acid gas of high density, normally adopt physical absorption method and chemical absorption method, the energy consumption height that these methods have, the toxicity that has is big, the solvent loss amount that has is big, the unstable easily degraded of absorption agent that has or catalyzer, the corrodibility that has is strong, and the leakage of these solvents pollutes the environment.Owing to there is above-mentioned shortcoming, the energy consumption of ammonia factory is increased, production cost improves.In addition, in the ammonia factory that produces bicarbonate of ammonia, whole liquefied ammonia of ammonia synthesis gained all are used for removing the carbonic acid gas of conversion gas, obtain the bicarbonate of ammonia product simultaneously, because the purposes of carbon ammonium is far away from liquefied ammonia factory, so influenced the economic benefit of these factories.PSA method of the present invention can not only remove the carbonic acid gas of exhausted major part, and reaches the various purification degree of depth, the various shortcoming that does not have absorption process to exist, and make factory a large amount of liquefied ammonia might be put on market, increase economic benefit.
As everyone knows, the PSA method very successfully is applied to extract highly purified hydrogen from hydrogen-rich mixed gas, existing many patents relate to and utilize the PSA method to come the purified ammonia synthetic gas over past ten years, because compare with traditional ammonia factory, flow process is simpler, capacity usage ratio is higher, for example: United States Patent (USP) 4375363, Deutsches Reichs-Patent 3335087 grades utilize the PSA method to remove impurity components such as denitrification, methane, carbon monoxide, carbonic acid gas from ammonia factory conversion gas, make pure hydrogen, be equipped with the synthetic hydrogen of stoichiometry nitrogen that comes from air separation facility again.Deutsches Reichs-Patent 3206513, English Patent 2126573, United States Patent (USP) 4592860, European patent 0157480,0183358 grade discloses the method for introducing the PSA purified ammonia factory conversion gas of excess air from hydrocarbon vapours air conversion process, to remove methane, carbon monoxide, carbonic acid gas and unnecessary nitrogen wherein, is mixed with hydrogen nitrogen than the synthetic gas that is 3, because these methods can be save expensive air separation facility, make it have higher utility.Yet the ammonia factory that produces bicarbonate of ammonia does not often have to increase the leeway of excess air in its gas making and shift conversion step, so will adopt above-mentioned patent to carry out bigger change to its upstream and downstream operation.Chinese patent publication number 1040354A discloses a kind of PSA method that reclaims carbonic acid gas from gaseous mixture, simultaneously can also provide the hydrogen nitrogen mixed gas that has removed most carbonic acid gas, but its concentration of carbon dioxide can not be lower than the 0.5%(molecular volume), re-use and bring many difficulties thereby make it return ammonia system.
The purpose of this invention is to provide a kind of excess air of not introducing in ammonia-preparing process, the PSA that need not add the expensive air separation facility of system again removes the method for carbonic acid gas in the conversion gas.
Another object of the present invention is that this PSA method can farthest reclaim hydrogen and the nitrogen in the unstripped gas, and to keep hydrogen nitrogen ratio be 3.
A further object of the invention is only to remove carbonic acid gas and boiling point than its high component from conversion gas, and makes its concentration in hydrogen nitrogen mixed gas be lower than the 0.5%(molecular volume).
Consider above-mentioned purpose and other purpose hereinafter will be described in detail the present invention, in claimed claim, specifically note its novel feature.
With coal or Sweet natural gas is the ammonia factory of raw material production carbon ammonium, and its typical technical process roughly is gasification or Sweet natural gas catalyzed conversion, normal pressure or pressurization conversion then, and through carbonization and washing decarburization, again through copper washing-refining, last high pressure synthetic ammonia.The present invention unstripped gas to be processed be gas after the conversion, its typical case forms as shown in Table 1:
Table one:
| (molecular volume) % | H 240-60 | N 210-22 | CO 1-3 | CH 41-4 |
| (molecular volume) % | O 2+Ar ＜1 | CO 224-30 | H 2S 200mg/m 3 | H 2O is saturated |
For PSA technology of the present invention, carbonic acid gas in the above-mentioned raw materials gas, hydrogen sulfide and water are to belong to the impurity component, must after by PSA, be removed substantially, in other words, these impurity components must be adsorbed agent and absorb, will be as the product of PSA operation and be not adsorbed the component that gets off, transport to the copper washing-refining operation, this shows that the PSA operation is to have replaced carbonization and water decarbonization process here.If the factory that has adopts wet method decarburizations such as propylene carbonate or hot potash liquid, PSA of the present invention can replace equally.
PSA technology of the present invention needs two or more (until ten) adsorption beds at least and forms a recycle system, and each adsorption bed in them once must experience following steps in the circulation successively.
(1) absorption (A): unstripped gas is sent into the adsorption bed feed end with top pressure and adsorb, optionally adsorb one or more easily components (for example carbonic acid gas, hydrogen sulfide, water etc.) of absorption, and in bed, set up the impurity absorption district, therefore, the component (for example hydrogen, nitrogen, methane, carbon monoxide etc.) that is difficult for absorption by whole adsorption bed and from the product end discharge, the impurity absorption district adsorption process constantly the product end to bed move, when the forward position of adsorption zone moves to the certain position of bed, end unstripped gas, stop absorption.
(2) pressure equalization is fallen and (is called for short equal pressure drop, ED): after the A step, from adsorption bed product end gas in the bed is discharged, because the bed internal pressure constantly descends in the discharge process, so impurity component absorb leading-edge also constantly moves to the product end of bed with adsorption zone, when just having moved to the product end, ends absorb leading-edge gaseous emission, at this moment, the impurity absorption district stays in the bed basically entirely, that is to say, expellant gas is substantially devoid of impurity component (for example carbonic acid gas, hydrogen sulfide, water etc.), the boosting of the bed that it is good that this strand gas can be used for regenerating.According to adsorptive pressure, processing power, the situation of bed number, equal pressure drop (maximum five times) is one or more times finished, promptly be divided into one or more (mostly being five most) pressure rating step by step step-down finish, pressure rating can abbreviate E1D, E2D, E3D, E4D, E5D as from high to low successively, and last all pressure drops, in also the minimum one-level of drop pressure power grade finished, the impurity absorption forward position should just in time arrive the product end of adsorption bed.
(3) reverse step-down (D): after above-mentioned ED step finishes, still residual gas then is to drain by the feed end of bed in the adsorption bed, until reaching atmospheric no better than degree, some of the impurity that adsorb this moment between adsorption cycle desorbed, and leaves bed with the gas of draining.
(4) (VC) finds time: regenerate more thoroughly in the bed in order to make, the method that employing vacuumizes, further reduce the dividing potential drop of impurity in the D step bed afterwards, remaining impurity component is drained from the feed end of bed, this process need make bed layer pressure reduce to 2～30KPa usually.
(5) the pressure equalization liter (is called for short equal voltage rise, ER): this step is corresponding with the ED step, promptly utilize the product gas of the adsorption bed discharge that is in the ED step, enter from the product end and to finish the adsorption bed that the VC step is in vacuum state, make its pressure that progressively raises, equally, this step can be divided once or five times at the most (being E1R, E2R, E3R, E4R, E5R) finish.
(6) (FR) finally boosts: because the ER step can't make adsorbent beds arrive adsorptive pressure, therefore the some of the product gas that need export with the adsorption bed that is in the A step is boosted to this adsorption bed from the product end, also useful raw materials gas boosts to this adsorption bed or product gas finally boosts to adsorption bed from feed end simultaneously from product end and unstripped gas from feed end, until reaching adsorptive pressure.
In the balanced PSA of four secondary pressures of the present invention system, reasonably arranged in order to make between every each step, permission is between E1D and the E2D step or between E1R and the E2R step, increase an isolation (IS) step, also can respectively increase an isolation step simultaneously between E1D and the E2D step and between E1R and the E2R.Those of ordinary skill in the art can both understand, and when carrying out this step, with this bed banded valve, all are in closing condition, make it temporarily isolated with other three beds.
The present invention is with described each patent of PSA method of using in ammonia factory conversion gas purifies is the same in front, and the technology of PSA all is at United States Patent (USP) 3430418,3564816, has carried out various improvement on 3986849 the basis.The skilled professional in present technique field can find out that each processing step of the present invention (comprising isolation step) and general PSA technology difference are to have replaced forward step-down and rinse step with evacuation step, promptly constitutes the feature of multi-bed vacuum transformation absorption.This improved benefit is to have avoided the product loss that causes because of flushing and has save that sorbent material partly that needs to increase for step-down forward in bed, thereby improved the rate of recovery of product gas significantly.People can recognize that this improvement is particularly conducive to the decarburization of conversion gas in the ammonia synthesizer, when the conversion gas with 0.1～3.0MPa during by PSA technology of the present invention, gas concentration lwevel can be controlled in the 0.5%(molecular volume in product gas) below, at this moment, the product atmospheric pressure is a little less than raw gas pressure 0.1MPa, and the rate of recovery of hydrogen can be greater than 95%, and the rate of recovery of nitrogen is greater than 90%, is easy to make hydrogen nitrogen than in being controlled at 2.8～3.5 scope by adjusting.Compare with general PSA technology, the rate of recovery of hydrogen can improve 2～5%, the rate of recovery of nitrogen can improve 30%, this shows, use PSA technology of the present invention, just need not from the external world to replenish nitrogen or introduce excess air from gas making workshop section, people can also see when using PSA technology of the present invention to replace traditional decarbonization process, need not its upstream process and lower procedure are done any change, very convenient.Compare with general PSA technology, the power consumption that increases by vacuumizing is remedied by the unstripped gas compression power consumption that its product high-recovery is saved.
Example one:
Adopt PSA technology three bed systems of the present invention, its processing step sees table two:
Conversion gas (it is formed as shown in Table 1) with 0.7MPa, the bed by pressure the highest (0.7MPa) wherein adsorbs, and all the other two beds all are in the regenerated different step, and three beds all load silica gel absorber.One time loop cycle is about 15 minutes, pressure equalization (E1D, when E1R) finishing, pressure is about 0.3MPa, reverse step-down terminal hour pressure is about 100KPa, when finding time to finish, pressure is 20KPa.Can obtain hydrogen nitrogen in this example than the gas mixture that is 3.08, it is that benchmark calculates with the molecular volume, contains 71.90% hydrogen, 23.31% nitrogen+argon, 1.48% methane, 2.83% carbon monoxide and 0.48% carbonic acid gas.Hydrogen recovery rate is 97.48%, and rate of recovery of nitrogen is 90.10%.
Example two:
Unstripped gas is formed and to be same as an example, and raw gas pressure is 1.2MPa, adopts four secondary pressure equalizing systems of PSA technology of the present invention, its processing step as shown in Table 3:
Gac in filling in four beds.Each circulation required time is 12 minutes.Pressure equalization terminal hour for the first time, bed layer pressure is about 0.66MPa, pressure equalization terminal hour for the second time, bed layer pressure is about 0.24MPa.Reverse step-down terminal hour pressure is about 200KPa, and the terminal hour pressure of finding time is 3KPa, and the end pressure that finally boosts is 1.2MPa.Can obtain hydrogen nitrogen ratio in this example is 3.27, and the hydrogen rate of recovery is 97.71%, and nitrogen recovery is 91.52%, hydrogeneous 73.45% in its product gas, nitrogen+argon 22.48%, methane 1.04%, carbon monoxide 2.67%, carbonic acid gas 0.36%.
Example three:
Adopt of the present invention six three pressure equalization systems, its processing step moves by table four, and raw gas pressure is 2.0MPa, the required time that circulates each time is 18 minutes, the bottom filling activated alumina of each, it accounts for the bed volume ratio is 0.2, all the other all load gac.For the first time the pressure at pressure equalization end is 1.65MPa, for the second time the pressure at pressure equalization end is 0.9MPa, the pressure of pressure equalization terminal hour is 0.4MPa for the third time, the pressure at reverse step-down end is 500KPa, the end pressure of finding time is 30KPa, and it is 2.0MPa that the pressure when finishing of finally boosting equals adsorptive pressure.
Can obtain the product gas that pressure is about 1.9MPa in this example, its hydrogeneous nitrogen ratio is 3.0, and the hydrogen rate of recovery is 96.49%, and nitrogen recovery is 93.69%, and is hydrogeneous 72.58% in its product gas, nitrogen+argon 24.24%, methane 0.30%, carbon monoxide 2.76%, carbonic acid gas 0.12%.
The PSA technology of above-mentioned explanation can make various changes and modifications in detail, all do not exceed to be proposed in the subordinate authority scope of the present invention.For example, the bed number of use; The number of times of pressure equalization; The equilibrium of pressure can be balanced completely or incomplete equilibrium, and it is different that promptly pressure equalization can make the pressure of two relevant adsorption beds eventually consciously; Can be in the scheme of table four, after the first time, pressure equalization was fallen, arrange again once to isolate, as the existing various examples of describing in front, can be according to circumstances and the change scheme, all within the scope of the invention.Those skilled in the art should be understood that in this area, the PSA system comprises various necessary pipelines, valve and other function uniies, with realize as the PSA operation in, adsorption bed switches to another from one in due course, and step switches to next step successively from a step.Should be understood that also as long as used any suitable sorbent material, it has selectivity to some component of various components contained in the material gas mixture, contain in the material gas mixture and be difficult for adsorbent component and easy adsorbent component, just can implement the present invention.For example, the zeolite molecular sieve of using always in the industry, gac, silica gel, activated alumina etc. all are applicable to PSA technological operation of the present invention.
Example as can be seen from the above description, the present invention proposes a kind of method that from conversion gas, removes carbonic acid gas and the component higher than carbonic acid gas boiling point, and make the gas composition that is not removed simultaneously, particularly hydrogen, nitrogen component have the quite high rate of recovery, make that substituting traditional decarbonization process with technology of the present invention demonstrates very big superiority, therefore, PSA technology of the present invention has positive meaning to the decarbonization process of transforming existing middle-size and small-size ammonia factory.
Claims (9)
1, a kind of pressure swing adsorption process that from synthetic-ammonia transformation gas, removes carbonic acid gas, it is characterized in that adopting multi-bed vacuum transformation absorption, experience absorption, all pressure drop, the reverse step-downs successively in circulation once of each adsorption bed, find time, all voltage rises, final desired each step of isallobaric absorbing process of boosting.
2,, it is characterized in that adsorption bed can be the combination of two or more (until ten) according to the pressure swing adsorption process of claim 1.
3,, it is characterized in that equal pressure drop number of times can divide once to five times with the variation of adsorption bed quantity to finish according to the pressure swing adsorption process of claim 1 and 2.
4,, it is characterized in that equal voltage rise number of times can divide once to five times with the variation of adsorption bed quantity to finish according to the pressure swing adsorption process of claim 1 and 2.
5, according to the pressure swing adsorption process of claim 1 and 2, its feature: when being four two equal systems, every once must increase isolation step in the circulation, can be arranged between the equal pressure drop of secondary, perhaps be arranged between the equal voltage rise of secondary, perhaps simultaneously respectively arranging an isolation step between the equal pressure drop of secondary and between the equal voltage rise of secondary.
6,, it is characterized in that available zeolite molecular sieve, gac, silica gel, activated alumina etc. make sorbent material according to the pressure swing adsorption process of claim 1 and 2.
7, according to the pressure swing adsorption process of claim 1 and 2, the adsorptive pressure when it is characterized in that adsorption step is controlled at 0.1～3.0MPa scope.
8, according to the pressure swing adsorption process of claim 1 and 2, the pressure-controlling when it is characterized in that evacuation step is in 2～30KPa scope.
9, according to the pressure swing adsorption process of claim 1 and 2, the step enabled production gas that it is characterized in that finally boosting finally boosts to adsorption bed from the product end, also useful raw materials gas finally boosts to adsorption bed from feed end, also can finally boost to adsorption bed simultaneously from feed end from product end and unstripped gas with product gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN91107278A CN1029552C (en) | 1991-08-24 | 1991-08-24 | Pressure swing adsorption process for removing carbon dioxide from ammonia plant shift gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN91107278A CN1029552C (en) | 1991-08-24 | 1991-08-24 | Pressure swing adsorption process for removing carbon dioxide from ammonia plant shift gas |
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| Publication Number | Publication Date |
|---|---|
| CN1069708A true CN1069708A (en) | 1993-03-10 |
| CN1029552C CN1029552C (en) | 1995-08-23 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN91107278A Expired - Lifetime CN1029552C (en) | 1991-08-24 | 1991-08-24 | Pressure swing adsorption process for removing carbon dioxide from ammonia plant shift gas |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1063095C (en) * | 1996-03-22 | 2001-03-14 | 杨皓 | Six-tower vacuum adsorption gas separating technology |
| CN1069687C (en) * | 1998-07-03 | 2001-08-15 | 李群柱 | Process for purification to obtain high-purity synthetic gas by adsorption |
| CN1089621C (en) * | 1996-06-10 | 2002-08-28 | 伍仁兴 | Multi-tower pressure-changeable gas-adsorption separation method |
| CN1315563C (en) * | 2003-06-06 | 2007-05-16 | 四川天一科技股份有限公司 | Adsorption stripping method for removing ethene and carbon dioxide from mixed gas |
| CN1891328B (en) * | 2006-05-10 | 2011-06-08 | 杨皓 | Low concentration adsorbable constituent variable-pressure adsorption and separation method |
| CN105967184A (en) * | 2016-05-10 | 2016-09-28 | 杨皓 | Process for combined production of ammonia and sodium carbonate by using shift gas |
-
1991
- 1991-08-24 CN CN91107278A patent/CN1029552C/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1063095C (en) * | 1996-03-22 | 2001-03-14 | 杨皓 | Six-tower vacuum adsorption gas separating technology |
| CN1089621C (en) * | 1996-06-10 | 2002-08-28 | 伍仁兴 | Multi-tower pressure-changeable gas-adsorption separation method |
| CN1069687C (en) * | 1998-07-03 | 2001-08-15 | 李群柱 | Process for purification to obtain high-purity synthetic gas by adsorption |
| CN1315563C (en) * | 2003-06-06 | 2007-05-16 | 四川天一科技股份有限公司 | Adsorption stripping method for removing ethene and carbon dioxide from mixed gas |
| CN1891328B (en) * | 2006-05-10 | 2011-06-08 | 杨皓 | Low concentration adsorbable constituent variable-pressure adsorption and separation method |
| CN105967184A (en) * | 2016-05-10 | 2016-09-28 | 杨皓 | Process for combined production of ammonia and sodium carbonate by using shift gas |
| CN105967184B (en) * | 2016-05-10 | 2018-02-23 | 杨皓 | A kind of technique of conversion gas combined production of ammonia and soda ash |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1029552C (en) | 1995-08-23 |
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