CN1100588C - Pressure swing adsorption process for extracting carbon monooxide as fuel from blast furnace waste gas - Google Patents
Pressure swing adsorption process for extracting carbon monooxide as fuel from blast furnace waste gas Download PDFInfo
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- CN1100588C CN1100588C CN97107736A CN97107736A CN1100588C CN 1100588 C CN1100588 C CN 1100588C CN 97107736 A CN97107736 A CN 97107736A CN 97107736 A CN97107736 A CN 97107736A CN 1100588 C CN1100588 C CN 1100588C
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Abstract
The present invention relates to two-step pressure swing adsorption technology for separating condensed carbon monoxide from mixed gas, particularly from exhaust gas of a blast furnace, which aims to achieve the purpose of extracting CO as fuel from exhaust gas of a blast furnace. Each adsorption bed is used for adsorption, uniform pressure reduction, reverse release, washing, uniform pressure increase and final pressure increase in a circulating mode in the first working procedure of the pressure swing adsorption method. After constituents with stronger adsorbability than carbon monoxide in mixed gas are adsorbed and removed, each adsorption bed is used for adsorption, uniform pressure reduction, positive release, washing, uniform pressure increase and final pressure increase in the second working procedure. Constituents with weaker adsorbability than carbon monoxide are removed, and condensed carbon monoxide is adsorbed.
Description
The present invention relates to from gaseous mixture the pressure swing adsorption technique, particularly the two-phase method pressure swing adsorption technique of separation and Extraction carbon monoxide from the blast furnace gas that Steel Plant's smelting process is produced of separation and purified gases.
Pressure swing adsorption process is a kind of the separation from gaseous mixture and the technology of purifying gas.Be a kind of gas that carries out at normal temperatures, solid phase physical adsorption process.Pressure swing adsorption also is the technology of less energy-consumption, non-environmental-pollution.Pressure swing adsorption has the feature of adsorption selectivity to different gas compositions according to sorbent material, big with loading capacity under high pressure (adsorptive pressure) to gas composition, and in the following little characteristics of loading capacity of low pressure (desorption pressures), alternately switch circulation technology by what absorption and desorb were formed, in order to the separation of realization gas composition.
The separation and recovery method of CO, industrial have Deep Cooling Method, solvent absorption, adsorption method of separation usually.Deep Cooling Method is because N2 and CO boiling point in its technical process complexity, gas mixture are approaching, and is difficult to separate, and therefore uses not general.Typical solvent absorption Cosorb method is the beginning of the seventies, succeeded in developing by U.S. Tenneco company, is widely adopted.But, the lyosorption that the Cosorb method is used, with the gas mixture that contains CO in impurity such as water, hydrogen sulfide, nitrogen contact for a long time after, receptivity can descend.Therefore, Cosorb method pretreatment technology complexity, absorbent regeneration energy consumption height.Adsorption separation technology is used industrial at the fifties latter stage, now has been widely used in H
2, N
2, O
2, CH
4Separation Deng gas is purified, and the purification of other industrial gasses.
Existing adsorption method of separation according to the difference of unstripped gas, and has different processing steps.Wherein, existing two-phase method transformation absorption purification CO technology is adsorbed successively through first section each adsorption bed of absorption process, all pressure drops, contrary putting, and flushing, all voltage rises, the circulation step that finally boosts are at first removed H
2O, CO
2Be better than the component of CO etc. adsorptive power; Enter second section absorption process then, each adsorption bed adsorbs successively, replaces, the contrary circulation step of putting, vacuumize, boosting, and carries out CO and N
2, O
2, H
2Deng the separation of component, remove the component that adsorptivity is weaker than carbon monoxide, occlusion and extract carbon monoxide obtains
COProduct.Existing two-phase method transformation adsorbing and extracting CO, the purification degree of CO is higher, but processing step complexity, complicated operation, facility investment height.
Steel Plant produce a large amount of blast furnace gas in the smelting process.It consists of:
Form: CO H
2CO N
2O
2+ Ar
V％：22～25 2～5 8～22 50～60 0.1
The blast furnace gas calorific value of this content is very low, has only 750 kcal/Nm
3About, can't be used as fuel, major part can only be as waste heat recovery, and irretrievable gas have to enter atmosphere, enters atmospheric CO every year and reaches more than 5,600,000 tons, not only environment has been caused severe contamination but also has wasted the valuable energy of CO.Existing blast furnace gas fails to obtain to utilize again, is because the CO concentration in the blast furnace gas is too low, therefore; improve blast furnace gas CO concentration, also just improved the calorific value of blast furnace gas, just can recycling; act as a fuel or other usefulness, all significant to protection environment and comprehensive utilization of C O.And act as a fuel, then need not highly purified CO, therefore just can adopt better simply technology.
Given this, the object of the present invention is to provide that a kind of technology is simpler, easy to operate, the pressure swing adsorption process of carrying dense carbon monoxide from blast furnace gas of less investment; Another object of the present invention is to provide a kind of CO of producing content is 66～85%, and combustion heat value is 2000kcal/Nm
3The pressure swing adsorption process of from blast furnace gas, carrying dense carbon monoxide of above fuel gas; Still a further object of the present invention is that CO content is dropped to is low as far as possible, reduces the pressure swing adsorption process of carrying dense carbon monoxide from blast furnace gas of environmental pollution.
The object of the present invention is achieved like this: on the technology basis of existing transformation absorption two-phase method purification CO, in its second section operation PSA-II, will be pressed onto normal pressure, and remove displacement, contrary strideing suddenly along strideing directly to put suddenly.Thereby the processing step of simplification flow process reduces the investment of device greatly.
The pressure swing adsorption process (referring to accompanying drawing) of from blast furnace gas, carrying dense carbon monoxide of the present invention, in the pressure swing adsorption system that constitutes by the first section operation (PSA-I) that each has at least two adsorption beds and second section operation (PSA-II) serial connection, with the sorbent material foreign gas in the fractionation by adsorption mixed gas optionally that is filled in the adsorption bed, it is characterized in that experiencing successively and contain absorption through each the adsorption bed circular flow of first section operation, all pressure drops, contrary putting, flushing, all voltage rises, the step of finally boosting, occlusion and removing after adsorptivity is better than the component of carbon monoxide in the gas mixture, experience successively through each the adsorption bed circular flow of second section operation again and contain absorption, all pressure drops, along putting, find time, all voltage rises, the step of finally boosting, remove the component that adsorptivity is weaker than carbon monoxide, occlusion and extract carbon monoxide.
The waste gas of using gas to discharge of first section above-mentioned operation rinse step from second section operation.
Sorbent material in the adsorption bed of first section above-mentioned operation is at least a in silica gel, gac, aluminium glue, the carbonaceous molecular sieve, and the sorbent material in the adsorption bed of second section operation is at least a in gac, carbonaceous molecular sieve, the zeolite molecular sieve.
The pressure of the adsorption step of first section above-mentioned operation is 0.1～1.2MPa, and the pressure of the adsorption step of second section operation is 0.1～1.1MPa, the pressure that vacuumizes step is-0.07～-0.098MPa.
The pressure swing adsorption process (referring to accompanying drawing) of carrying dense carbon monoxide from carbon mono oxide mixture of the present invention constitutes pressure swing adsorption system by first section operation (PSA-I) and second section operation (PSA-II) serial connection, and the concentration process of its CO is as follows.
Blast furnace gas is by introducing outside the system, by pipeline in pressure 0.1～1.2MPa (gauge pressure), enter the adsorption bed of first section operation under 20～40 ℃ of the room temperatures, first section operation is according to the difference of unstripped gas composition, tolerance, pressure, (3～10) form by a plurality of adsorption beds more than three or three, and, be equipped with corresponding time variable control valve according to adsorption bed quantity and processing step.The sorbent material of filling is one or more in special silica gel, gac, aluminium glue, the carbonaceous molecular sieve in each adsorption bed, to remove H
2O, CO
2And sulfide.Contain N in the work in-process gas that obtains
2And small amount of H
2And O
2+ Ar enters the adsorption bed of second section operation.The CO that in first section operation adsorption bed, adsorbs
2Put and the backwashing manner desorb by contrary etc. component, purge gas comes from second section the suitable waste gas of putting.
First section operation is purpose with the component that removes adsorptivity and be better than CO, and each adsorption bed is finished a cyclical operation, needs experience absorption, all pressure drops, reverse pressures, flushing, equal voltage rise, the final step of boosting of putting, and a plurality of adsorption beds are alternately finished above-mentioned processing step.Each adsorption bed is all being carried out mutually different step at one time, at any time, always there are one or more adsorption beds to be in adsorption step, and under the substantially invariable situation of pressure, with the work in-process gas that obtains, transfer to the adsorption bed of second section operation through pipeline.Below each step of this operation is illustrated.
Absorption (A): unstripped gas enters adsorption bed, the H in the unstripped gas continuously and stably under certain pressure (0.1～2.0MPa gauge pressure)
2O, CO
2, sulfide etc. is adsorbed, stay in the adsorption bed, and the CO that is adsorbed, H
2, O
2, N
2, the attached bed of outflow suction meeting such as Ar goes second section operation, carries out separating of CO and other component.When adsorption bed after adsorbing impurity after a while, sorbent material is basically by CO
2, H
2Saturated Deng impurity institute, for being regenerated, sorbent material need enter next step operation.
All pressure drops (ED): all to be the adsorption bed of finishing adsorption step put the process of pressure to other adsorption bed that need boost to voltage drop step, and all voltage drop step can reclaim the useful component in the adsorption bed.Equal voltage drop step can be divided into 1～5 time to be finished, and is called once all pressure drops, the equal pressure drop of secondary, three equal pressure drops, four equal pressure drops, five equal pressure drops.In concrete technological process, the equal pressure drop number of times that is adopted is decided on raw gas pressure and composition and adsorption bed quantity.
Contrary put (D): the promptly reverse pressure of putting.Putting pressure is that adsorption bed pressure is reduced, and makes the process of impurity component (component that need the remove) desorb of adsorbing in the adsorption bed.Reverse end finger air flow direction and the flow of feed gas of putting is to opposite.
Flushing (P): flushing is the gas purging adsorption bed with component free from foreign meter, makes the process of the abundant desorb of impurity component.Purge gas comes from the waste gas of second section operation.
All voltage rises (ER): all voltage rise is a process of utilizing the equal pressure drop gas of another tower that adsorption bed is boosted.Equal voltage rise step can be divided into 1～5 time to be finished, and is called once all voltage rises, the equal voltage rise of secondary, three equal voltage rises, four equal voltage rises, five equal voltage rises.In concrete technological process, the equal voltage rise number of times that is adopted is decided on raw gas pressure and composition.All voltage rise is with all the pressure drop number of times is corresponding.
(FR) finally boosts: this step is to make adsorption bed pressure be raised to the process of adsorptive pressure.
After finishing above-mentioned steps, adsorption bed has been finished the cyclical operation of one-period, and the processing step of each adsorption bed experience is identical, just staggers mutually in time, at any time all there is an adsorption tower carrying out the adsorption step operation with assurance, thus the continuous operation of assurance device.
Second section operation is serially connected in after first section operation.According to the difference of unstripped gas composition, tolerance, pressure, form by four or more a plurality of adsorption beds (4～12), and, be equipped with corresponding time variable control valve according to adsorption bed quantity and processing step.Be filled with gac, molecular sieve or carbon molecular sieve adsorbent in the adsorption bed, look blast furnace gas form may be wherein one or more.In the adsorption bed of second section operation, sorbent material carries out selective adsorption to CO, and CO stays in the adsorption bed, other H
2, N
2, O
2, Ar is from the exit end discharge section, returns first section operation through pipeline, as the purge gas of first section operation adsorbent reactivation, the gas emptying after the flushing wherein is mainly H
2+ N
2+ CO
2The CO of occlusion in adsorption bed obtains spissated CO product with the desorb of vacuum take-off mode, and this products C O is greater than 66% above concentration (suitable 2000kcal/Nm
3) export for the user and make fuel or other purposes.
First section operation is to obtain the CO product, in the circulation each time of second section operation, each adsorption bed all will experience absorption, all pressure drops, the suitable processing step of putting, find time, boost, and no matter adopts several adsorption beds combinations, all alternately carry out these processing steps, so that the output of CO product continous-stable.Now each step is explained as follows:
Absorption (A): from the work in-process pneumatic transmission of first section operation (PSA-I) output to this workshop section, unstripped gas as (PSA-2), enter from the adsorption bed inlet end, wherein CO is selected is adsorbed on the sorbent material, and other component discharges the PSA-I operation as absorption waste gas from the adsorber top.The purge gas that a part is used as the adsorbent reactivation of PSA-I operation.This step has realized that CO is difficult for separating of absorbed component with other.
All pressure drops (ED): this step and equal voltage drop step
Along putting (PP): promptly forward put pressure.The direction of carrying out along absorption is depressured to normal pressure, and step-down gas imports absorption waste gas, and by outside first section operation discharge system.
(VC) finds time: when adsorption bed pressure is reduced to normal pressure, further reduce the pressure of adsorption bed by the power of vacuum pump, withdrawing gas is spissated CO product, and output system is for the user.After this step was finished, the agent of adsorption bed internal adsorption was also regenerated and is finished, and prepared to carry out next step cyclical operation.
(FR) finally boosts: after evacuation step is finished, utilize absorption waste gas that this bed is boosted.
The pressure swing adsorption process of carrying dense carbon monoxide from blast furnace gas of the present invention is a raw material with the blast furnace gas, adopts first section operation to remove the H that adsorptive power is better than CO
2O, CO
2Etc. component, second section operation removed the N that adsorptive power is weaker than CO
2, O
2, H
2Etc. component, and, obtain spissated CO product through the step-down mode of finding time then by occlusion CO.Compare with existing two-phase method, removed displacement, the reverse pressure step of putting, have that technology is simple, operation steps is simplified, and then reduce the investment advantage of device greatly.
The present invention can be a raw material with the blast furnace gas, and producing CO content is 66～85%, and combustion heat value is 2000kcal/Nm
3The CO fuel of above high heating value.CO content is extremely low in its combustion gas, and its content is below 9%, thereby has reduced environmental pollution.
Below, with embodiment and accompanying drawing thereof the present invention is further described again.
Brief description of drawings.
Fig. 1 is a kind of process flow sheet of carrying the pressure swing adsorption process of dense carbon monoxide from blast furnace gas of the present invention.Show that first section operation is that three, second section operation is four technical process.
Fig. 2 is the gas flow figure of first section each step of operation of Fig. 1.
Fig. 3 is the gas flow figure of second section each step of operation of Fig. 1.
Fig. 4 is the pressure trend figure of first section each step of operation of Fig. 1.
Fig. 5 is the pressure trend figure of second section each step of operation of Fig. 1.
Fig. 6 is another kind of the present invention is carried the pressure swing adsorption process of dense carbon monoxide from blast furnace gas a process flow sheet.Show that first section operation is that six, second section operation is eight technical process.
Fig. 7 is the gas flow figure of first section each step of operation of Fig. 6.
Fig. 8 is the gas flow figure of second section each step of operation of Fig. 6.
A kind of pressure swing adsorption process of from blast furnace gas, carrying dense carbon monoxide of the present invention, unstripped gas is a blast furnace gas, its composition:
Form: CO
2O
2CO H
2N
2
V％：20.61 0.3 22.76 1.46 54.87
This pressure swing adsorption process adopts common pressure swing adsorption system, technical process as shown in Figure 1, first section operation PSA-I adopts three one equal technologies, second section operation PSA-II adopts four one equal technologies.Corresponding relation between each adsorption bed processing step of first section operation and second section operation is respectively shown in table 1, table 2.The gas flow of the processing step of first section operation and second section operation is respectively as Fig. 2, shown in Figure 3, among the figure only to each the step gas flow of A bed as mark, the air flow direction between other each is similar to the A bed, so do not mark.
First section process operations pressure is at 0.1～0.35MPa, and second section working pressure operated in-0.08～0.3MPa scope.Each step pressure change is respectively as Fig. 4, shown in Figure 5.
First section operation PSA-I has adsorption bed IA, IB, the IC of three tower structures, and raw material tracheae 1I that is communicated with each adsorption bed and inlet valve separately are 1-IA, 1-IB, 1-IC; Semifinished tube 2I that is communicated with each adsorption bed and outlet valve 2-IA, 2-IB, 2-IC separately; Contrary pipe 3I and contrary valve 3-IA, 3-IB, the 3-IC put separately put that is communicated with each adsorption bed; What be communicated with each adsorption bed all presses final rise pipe 5I and variable valve 5-1 and separately all pressures final rise valve 5-IA, 5-IB, 5-IC; Washpipe 6I that is communicated with each adsorption bed and variable valve 6-I thereof and separately flush valve 6-IA, 6-IB, 6-IC.The sorbent material of filling is silica gel or gac in each adsorption bed.
Second section operation PSA-II, adsorption bed IIA, IIB, IIC, IID that four tower structures are arranged, the semifinished tube 1I of first section operation PSA-I and the semifinished tube III that is communicated with each adsorption bed of this operation and variable valve 1-II and separately inlet valve 1-IIA, 1-IIB, 1-IIC, 1-IID continue; The absorption waste pipe 2II that is communicated with each adsorption bed and outlet valve 2-IIA, 2-IIB separately, 2-IIC, 2-IID 2-2D; Product pipe 3II that is communicated with each adsorption bed and outlet valve 3-IIA, 3-IIB, 3-IIC, 3-IID separately; What be communicated with each adsorption bed manages 4II and suitable valve 4-IIA, 4-IIB, 4-IIC, the 4-IID put separately along putting; The all pressures that are communicated with each adsorption bed finally boost pipe 5II and variable valve 5-II thereof and the final back-up valve 5-IIA of all pressures separately, 5-IIB, 5-IIC, 5-IID; Be provided with vacuum pump 7 among the product pipe 3II.The sorbent material of filling is a zeolite molecular sieve in each adsorption tower.
This pressure swing adsorption system, under computer instruction, each valve supporting with technological process automaticallyes switch execution by the set algorithm of processing requirement.
Blast furnace gas is under about 0.35MPa pressure, enter first section operation PSA-I of the present invention, according to the algorithm of table 1, this operation adsorption bed, every loop cycle by absorption A, all pressure drop ED, contrary put D, flushing P, all voltage rise ER, finally six steps of FR of boosting are formed.In three absorption, remove the strong absorbed component H in the gas
2O, CO
2Etc. foreign gas, be sent to second section operation PSA-II of the present invention as work in-process.Under 0.3MPa pressure, enter the adsorption bed of second section operation, according to the continuous cyclical operation of the algorithm of table 2, the every loop cycle of this operation adsorption bed by absorption A, all pressure drop ED, along put PP, the VC that finds time, all voltage rise ER, finally six steps of FR of boosting are formed.To remove the most of weak absorption impurity composition N in the work in-process gas
2, H
2, Ar+O
2Deng, from the adsorption bed solid-phase adsorbent, obtain to concentrate the CO product at last by the mode of finding time.Under the control of computer, blast furnace gas is constantly imported during the native system operation, and spissated products C O exports continuously.
Present embodiment can obtain products C O purity 〉=66%, promptly reaches combustion heat value 2000kcal/Nm
3More than, the CO rate of recovery becomes available industrial fuel more than 85%.CO in the discharging gas reduces to below 8% from 22～25%.
Embodiment 2:
Another kind of the present invention is carried the pressure swing adsorption process of dense carbon monoxide from blast furnace gas, similar with embodiment 1, and first section operation PSA-I is six one equal technologies, and second section operation PSA-II is eight one equal technologies.Whenever all have two adsorption beds to be in the charging adsorbed state simultaneously, its technical process as shown in Figure 6.
Unstripped gas is Steel Plant's blast furnace gas, and it is formed with embodiment 1:
Form: CO
2O
2CO H
2N
2
V％：20.61 0.3 22.76 1.46 54.87
This pressure swing adsorption process adopts common pressure swing adsorption system, technical process as shown in Figure 1, first section operation PSA-I adopts six one equal technologies, second section operation PSA-II adopts eight one equal technologies.Corresponding relation between each adsorption bed processing step of first section operation and second section operation is respectively shown in table 3, table 4.The gas flow of the processing step of first section operation and second section operation is respectively as Fig. 7, shown in Figure 8, among the figure only to each the step gas flow of A bed as mark, the air flow direction between other each is similar to the A bed, so do not mark.
First section process operations pressure is at 0.1～0.35MPa, and second section working pressure operated in-0.08～0.3MPa scope.Each step pressure change is respectively as Fig. 4, shown in Figure 5.
First section operation PSA-I has adsorption bed IA, IB, IC, ID, IE, the IF of six tower structures, and raw material tracheae 1I that is communicated with each adsorption bed and inlet valve separately are 1-IA, 1-IB, 1-IC, 1-ID, 1-IE, 1-IF; Semifinished tube 2I that is communicated with each adsorption bed and outlet valve 2-IA, 2-IB, 2-IC, 2-ID, 2-IB, 2-IF separately; Contrary pipe 3I and contrary valve 3-IA, 3-IB, 3-IC, 3-ID, 3-IE, the 3-IF put separately put that is communicated with each adsorption bed; All pressures final rise pipe 5I that is communicated with each adsorption bed and variable valve 5-I thereof and separately all pressures final rise valve 5-IA, 5-IB, 5-IC, 5-ID, 5-IE, 5-IF; Washpipe 6I that is communicated with each adsorption bed and variable valve 6-I thereof and separately flush valve 6-IA, 6-IB, 6-IC, 6-ID, 6-IE, 6-IF.
Second section operation PSA-II, adsorption bed IIA, IIB, IIC, IID, IIE, IIF, IIG, IIH that eight tower structures are arranged, the semifinished tube 1I of first section operation PSA-I continues, and the semifinished tube 1II that is communicated with each adsorption bed of this operation and variable valve 1-II and separately inlet valve 1-IIA, 1-IIB, 1-IIC, 1-IID, 1-IIE, 1-IIF, 1-IIG, 1-IIH; Absorption waste pipe 2II that is communicated with each adsorption bed and outlet valve 2-IIA, 2-IIB, 2-IIC, 2-IID, 2-IIE, 2-IIF, 2-IIG, 2-II separately; Product pipe 3II that is communicated with each adsorption bed and outlet valve 3-IIA, 3-IIB, 3-IIC, 3-IID, 3-IIE, 3-IIF, 3-IIG, 3-IIH separately; What be communicated with each adsorption bed manages 4II and suitable valve 4-IIA, 4-IIB, 4-IIC, 4-IID, 4-IIE, 4-IIF, 4-IIG, the 4-IIH put separately along putting; The all pressures that are communicated with each adsorption bed finally boost pipe 5II and variable valve 5-II thereof and the final back-up valve 5-IIA of all pressures separately, 5-IIB, 5-IIC, 5-IID, 5-IIE, 5-IIF, 5-IIG, 5-IIH; Be provided with vacuum pump 7 among the product pipe 3II.
This pressure swing adsorption system, under computer instruction, each valve supporting with technological process automaticallyes switch execution by the set algorithm of processing requirement.
Unstripped gas is compressed to 0.5MPa, enter the PSA-I operation at normal temperatures, through removing CO
2, H
2Behind the impurity such as O, sulfide; Work in-process gas enters PSA-II operation, H
2, N
2Separate with CO, carry dense CO.The CO that carries after dense obtains by the mode of vacuumizing, and sorbent material obtains regeneration simultaneously.
The PSA-I operation is pressed the operation of the equal processing step of six one shown in the chart 3, this operation adsorption bed, every loop cycle by absorption A, all pressure drop ED, contrary put D, flushing P, all voltage rise ER, finally six steps of FR of boosting are formed.Fig. 7 is the gas flow that example illustrates each algorithm with adsorption bed IA, and the gas flow between other each adsorption bed is similar to the A bed, so marking explanation in addition not.
Being in operation always has two adsorption beds to be in charging, the adsorption step of output work in-process gas, and all the other four adsorption beds are in the different step of absorption regeneration.Press the job step preface of table 3, just can make work in-process gas continous-stable transport to the PSA-II operation, as the unstripped gas of PSA-II operation.The sorbent material of filling is activated alumina and silica gel in each adsorption bed of this operation.About 720 seconds of the loop cycle that is experienced.Adsorptive pressure is at 0.5MPa.Adsorbent reactivation is by equal pressure drop, all press end pressure be～0.25MPa another mistake puts to normal pressure, finishes through rinse step under normal pressure then.
The PSA-II operation is pressed the processing step operation of table 4, the every loop cycle of this operation adsorption bed by absorption A, all pressure drop ED, along put PP, the VC that finds time, all voltage rise ER, finally six steps of FR of boosting are formed.Fig. 8 is each algorithm gas flow of illustration with adsorption bed IIA, and the gas flow between other each is similar to the A bed, so marking explanation in addition not.
Being in operation always has two adsorption bed chargings to be in adsorption step, and adsorption step carries out under 0.4MPa pressure, to remove the weak absorption impurity composition N in the work in-process gas
2, H
2, portion C H
4With Ar etc.Absorption finishes the back all presses with another adsorption bed of just finding time to finish, and this equal pressure drop gas carries out equal voltage rise to another adsorption bed.All press end pressure to be about 0.18MPa (gauge pressure).All carry out after the pressure drop dropping to normal pressure 0MPa (gauge pressure) along putting whole adsorption bed pressure, the gas of absorption front end is further separated along strideing suddenly.Last step-down mode to find time, the about 0～0.08MPa of evacuation pressure obtains spissated CO product, and sorbent material is regenerated simultaneously.Mode with equal voltage rise rises to～0.118MPa this adsorption bed then, boosts to adsorptive pressure 0.4MPa with absorption waste gas again and carries out next round-robin operation.In eight adsorption beds, all load zeolite molecular sieve and make sorbent material.About 960 seconds of the cycle of being experienced.
This example can obtain product and concentrate CO purity＞75%, the CO rate of recovery＞and more than 80%.CO in the discharging gas reduces to below 9% from 22～25%.
Table 1 PSA-I operation three bed process step corresponding relation figure
| 1 | 2 | 3 | 4 | 5 | 6 | 7 | 8 | 9 | 10 | 11 | 12 | |
| IA | A | ED | D | P | ER | FR | ||||||
| IB | ER | FR | A | ED | D | P | ||||||
| IC | ED | D | P | ER | FR | A | ||||||
Table 2 PSA-II operation four bed process step corresponding relations
| 1 | 2 | 3 | 4 | 5 | 6 | 7 | 8 | 9 | 10 | 11 | 12 | 13 | 14 | 15 | 16 | ||
| IIA | A | ED | PP | VC | ER | FR | |||||||||||
| IIB | ER | FR | A | ED | PP | VC | |||||||||||
| IIC | VC | ER | FR | A | ED | PP | |||||||||||
| IID | ED | PP | VC | ER | FR | A | |||||||||||
Table 3 PSA-I operation six bed process step corresponding relation figure
| 1 | 2 | 3 | 4 | 5 | 6 | 7 | 8 | 9 | 10 | 11 | 12 | ||
| IA | A | ED | D | P | ER | FR | |||||||
| IB | FR | A | ED | D | P | ER | FR | ||||||
| IC | ER | FR | A | ED | D | P | |||||||
| ID | P | ER | FR | A | ED | D | |||||||
| IE | ED | D | P | ER | FR | A | |||||||
| IF | A | ED | D | P | ER | FR | A | ||||||
Table 4 PSA-II operation eight bed process step corresponding relation figure
| 1 | 2 | 3 | 4 | 5 | 6 | 7 | 8 | 9 | 10 | 11 | 12 | 13 | 14 | 15 | 16 | |||
| IIA | A | ED | PP | VC | ER | FR | ||||||||||||
| IIB | FR | A | ED | PP | VC | ER | FR | |||||||||||
| IIC | ER | FR | A | ED | PP | VC | ||||||||||||
| IID | VC | ER | FR | A | ED | PP | VC | |||||||||||
| IIE | VC | ER | FR | A | ED | PP | ||||||||||||
| IIF | PP | VC | ER | FR | A | ED | PP | |||||||||||
| IIG | ED | PP | VC | ER | FR | A | ||||||||||||
| IIH | A | ED | PP | VC | ER | FR | A | |||||||||||
Claims (4)
1, from blast furnace gas, carry the pressure swing adsorption process of dense carbon monoxide, in the pressure swing adsorption system that constitutes by the first section operation (PSA-I) that each has at least two adsorption beds and second section operation (PSA-II) serial connection, with the sorbent material foreign gas in the fractionation by adsorption mixed gas optionally that is filled in the adsorption bed, it is characterized in that experiencing successively and contain absorption through each the adsorption bed circular flow of first section operation, all pressure drops, contrary putting, flushing, all voltage rises, the step of finally boosting, occlusion and removing after adsorptivity is better than the component of carbon monoxide in the gas mixture, experience successively through each the adsorption bed circular flow of second section operation again and contain absorption, all pressure drops, along putting, find time, all voltage rises, the step of finally boosting, remove the component that adsorptivity is weaker than carbon monoxide, occlusion and extract carbon monoxide.
2, pressure swing adsorption process according to claim 1 is characterized in that the waste gas of the usefulness gas of said first section operation rinse step from second section operation discharge.
3, pressure swing adsorption process according to claim 1 and 2, sorbent material in the adsorption bed of the said first section operation of its feature is at least a in silica gel, gac, aluminium glue, the carbonaceous molecular sieve, and the sorbent material in the adsorption bed of second section operation is at least a in gac, carbonaceous molecular sieve, the zeolite molecular sieve.
4, pressure swing adsorption process according to claim 3, the pressure that it is characterized in that the adsorption step of said first section operation is 0.1～1.2MPa, the pressure of the adsorption step of second section operation is 0.1～1.1MPa, the pressure that vacuumizes step is-0.07～-0.098MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97107736A CN1100588C (en) | 1997-10-24 | 1997-10-24 | Pressure swing adsorption process for extracting carbon monooxide as fuel from blast furnace waste gas |
Applications Claiming Priority (1)
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| CN97107736A CN1100588C (en) | 1997-10-24 | 1997-10-24 | Pressure swing adsorption process for extracting carbon monooxide as fuel from blast furnace waste gas |
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| CN1215625A CN1215625A (en) | 1999-05-05 |
| CN1100588C true CN1100588C (en) | 2003-02-05 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101396632B (en) * | 2008-10-27 | 2011-08-24 | 四川亚连科技有限责任公司 | Multi-stage absorption, regeneration and purification method of polysilicon tail gas |
| CN101549240B (en) * | 2009-04-23 | 2011-05-04 | 天津大学 | Method for absorbing methane in condensed coal bed gas through pressure varying mode including carbon dioxide replacement |
| US8177886B2 (en) * | 2009-05-07 | 2012-05-15 | General Electric Company | Use of oxygen concentrators for separating N2 from blast furnace gas |
| CN101653688B (en) * | 2009-06-24 | 2013-07-10 | 成都华西工业气体有限公司 | Process flow for removing CO2 and H2S in gas mixture |
| CN102326859B (en) * | 2011-06-30 | 2012-12-19 | 红云红河烟草(集团)有限责任公司 | Method for extracting tobacco essence perfume from cigarette processing waste gas |
| CN104610087B (en) * | 2014-11-28 | 2017-01-18 | 西南化工研究设计院有限公司 | Device and method for purifying yellow phosphorus tail gas and continuously synthesizing oxamide |
| CN105817117B (en) * | 2016-04-18 | 2018-09-18 | 四川天一科技股份有限公司 | A kind of efficient pressure-changeable gas-adsorption separation method |
| CN106943842A (en) * | 2017-04-19 | 2017-07-14 | 成都赛普瑞兴科技有限公司 | A kind of pressure-changeable gas-adsorption separation method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4732577A (en) * | 1986-04-14 | 1988-03-22 | Osaka Sanso Kogyo Ltd. | Process for separating carbon monoxide having substantially constant purity |
| CN1145269A (en) * | 1996-02-14 | 1997-03-19 | 成都华西化工研究所 | Method and appts. for reclaiming CO and hydrogen from smelting discharge gas |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4732577A (en) * | 1986-04-14 | 1988-03-22 | Osaka Sanso Kogyo Ltd. | Process for separating carbon monoxide having substantially constant purity |
| CN1145269A (en) * | 1996-02-14 | 1997-03-19 | 成都华西化工研究所 | Method and appts. for reclaiming CO and hydrogen from smelting discharge gas |
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| CN1215625A (en) | 1999-05-05 |
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