CN103736361A - Pressure swing adsorption unit device, pressure swing adsorption system and adsorption separation method thereof - Google Patents
Pressure swing adsorption unit device, pressure swing adsorption system and adsorption separation method thereof Download PDFInfo
- Publication number
- CN103736361A CN103736361A CN201310664545.8A CN201310664545A CN103736361A CN 103736361 A CN103736361 A CN 103736361A CN 201310664545 A CN201310664545 A CN 201310664545A CN 103736361 A CN103736361 A CN 103736361A
- Authority
- CN
- China
- Prior art keywords
- adsorption tower
- tower
- gas
- pressure
- adsorption
- 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.)
- Pending
Links
Images
Landscapes
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention discloses a pressure swing adsorption unit device, a pressure swing adsorption system and an adsorption separation method thereof, the adsorption unit device is a composite structure comprising a main adsorption tower 1 and at least one vice adsorption tower 5 which are successively arranged in an end-to-end connection mode, program-controlled valves 3 are respectively arranged between the adsorption towers which are in end-to-end connection, the main adsorption tower 1 is provided with a feed gas inlet pipe 6, and a final stage vice adsorption tower is provided with a treated-gas outlet pipe 10. The pressure swing adsorption system of the invention comprises two or more than two pressure swing adsorption unit devices, the pressure swing adsorption unit devices are connected in a parallel connection manner, and are connected with each other through pipelines, the pipelines are provided with the program-controlled valves. By use of the pressure swing adsorption system disclosed by the present invention, one and / or a variety of product gas can be separated from a mixed gas, compared with a traditional-structure pressure swing adsorption system, the content, the purity and the purification degree are improved and adjusted, and the investment and the floor area are saved.
Description
Technical field
The present invention relates to mist separation technology field, relate in particular to a kind of psa unit device, pressure swing adsorption system and adsorption separating method thereof.
Background technology
Pressure-variable adsorption (PSA) thus method is a kind ofly can carry out separating treatment to mist and obtain the wherein effective measures of a certain or some specific components gas product with high concentration and/or high purification mode, existing increasing research and application, to reach the further saving energy and/or resource be fully used.Particularly can obtain high-load and/or highly purified easy absorbed component and two kinds of gas products of difficult absorbed component simultaneously.For example, ZL92113609.9 Chinese patent had just once proposed a kind of " producing the gas separation method by pressure swing adsorption of two kinds of high-purities and high yield gas product " simultaneously.The Chinese patent literature that is CN1063351C at notification number " improves the method for equalizing frequency in process of pressure-swing adsorption ", by increasing the mode of all pressing number of times, be that a kind of can solution improved the purity of two kinds of gas products and the effective measures of yield aspect simultaneously, but energy consumption is higher.
At notification number, be that CN1172737C and publication number are CN1347747A, 1342509A, 1334135A, 1546205A, 1583221A, and in many Chinese patent literatures such as 1557528A, the pressure swing absorption process of a kind of two-part and syllogic has been proposed respectively again, adopted by two covers by several adsorption towers composition (or three covers) respectively independently pressure swing adsorption system mutually connect, the pressure-swing absorption process of every cover (section) system is all operation operations in the usual way separately, complete corresponding absorption, all press and the step such as desorb, obtain respectively easily absorption and two kinds of products of difficult absorbed component gas.Its feature is, latter one section (and the back segment in syllogic system) pressure-swing absorption process in its two-part system is take the working off one's feeling vent one's spleen as raw material of system the last period, working off one's feeling vent one's spleen and further carry out purification system the last period; In desorption process, after the pressure equalizing of rear one section of adsorption system finishes, available gas in adsorption tower is directly emptying not, but directly or by intermediate buffer tank, return it to again the last period adsorption system and reclaimed, thereby reach, improve the rate of recovery of two kinds of gas products and the object of degree of purification.For example, with the processing of two-part adsorption system, containing CO
2and H
2during etc. the mist of component, one section system is used for removing and purifying CO
2gas product, middle CO works off one's feeling vent one's spleen
2dense; Two sections of systems, take one section outlet gas as raw material, further separate the CO reclaiming wherein
2, improve its middle H that works off one's feeling vent one's spleen
2degree of purification.The serially connected pressure swing adsorption system of two sections of this employings or multistage carries out separating treatment to mist, can improve the rate of recovery and the degree of purification of easy absorption and two kinds of component gas products of difficult absorption, and the loss with desired gas component product is little, power consumption is extremely low, and easy and simple to handle, elasticity is large, the advantages such as the low and automaticity height of operating cost, but because its each section of pressure-variable adsorption separating treatment process is to carry out in the adsorption tower system of independent operating respectively, therefore the required floor space of whole treatment system increases considerably, simultaneously number of devices and the also corresponding increase of investment such as supporting required sequencing valve and intermediate buffer tank in each system.
Described in Granted publication CN100493671C patent documentation, two sections of pressure swing absorption process are applied in conversion gas decarburization, products C O
2purity 98.5%(V), CO in gas product
2content is less than 0.2%(V), hydrogen yield is greater than 98.5%(V), rate of recovery of nitrogen is greater than 95%(V), CO
2the rate of recovery is greater than 70%.CO
2purity and gas product in CO
2content meets need of production, but hydrogen and rate of recovery of nitrogen are on the low side, causes the loss of available gas and energy; And the rate of recovery of carbon dioxide is only greater than 70%, causing the enterprise take natural gas as raw material cannot be urea by more Ammonia Production, causes liquefied ammonia to remain in a large number.
This shows that the adsorption tower unit in the pressure swing adsorption system of above-mentioned existing report and use is the version of common single adsorption tower.Various pressure swing absorption process are all also research and improvement of carrying out based on this kind of form adsorption tower unit, are therefore subject to this traditional form single adsorption tower cellular construction self to limit to the problem and shortage of bringing and be difficult to have more quantum jump.Meanwhile, the rate of recovery of available gas is on the low side, causes production cost to increase, and the emptying of carbon dioxide also damages environment.
Summary of the invention
In order to solve the deficiency of existing pressure-swing absorption apparatus, first the present invention will provide a kind of new psa unit device.On this basis, the present invention also adopts by further providing the pressure swing absorption process that carries out mist separation by the pressure swing adsorption system that contains said absorbing unit device.
The psa unit device of the said pressure swing adsorption system of the present invention, be respectively arranged with equally raw material gas inlet and gas vent after treatment with sequencing valve, the serially connected composite construction that this absorbing unit device is comprised of the main adsorption tower setting gradually with head and the tail connected mode and at least one secondary adsorption tower, between end to end each adsorption tower, be respectively equipped with the main sequencing valve of break-make between control tower, main adsorption tower is provided with raw material gas inlet, and the secondary adsorption tower of final stage is provided with gas vent after treatment.
On the basis of above-mentioned basic structure, flexibility and adaptability in the time of each operating unit need to mutually being combined, be adjusted according to difference in pressure-variable adsorption processing procedure for further increasing, between the outlet of at least one the said adsorption tower in said structure and its adjacent main sequencing valve, be also provided with at least one tributary circuit with sequencing valve, and/or be also provided with at least one tributary circuit with sequencing valve between the import of at least one said adsorption tower and its adjacent main sequencing valve.
Remove according to special requirement, in said psa unit device, can arrange outside the secondary adsorption tower of two-stage or more multistage mutual series winding, in the psa unit device of said structure of the present invention, said secondary adsorption tower is generally set to one and can satisfies the demand, and can obtain satisfied effect.
Pressure swing adsorption system of the present invention, comprises two or more psa unit devices, and each presses absorbing unit device to connect in parallel, between them, by pipeline, connects, and pipeline is provided with sequencing valve.
The pressure swing adsorption system that employing contains the above-mentioned absorbing unit device of the present invention carries out pressure swing absorption process basic operation and the process of mist separation, there is no essential distinction with operation and the process of conventional pressure swing adsorption system.At least including in the pressure swing adsorption system of two above-mentioned form absorbing units of the present invention, each absorbing unit is equally with sequential interlace mode, make respectively pending mist through following absorption, all press and desorption process, according to the absorption complexity between each gas component and corresponding adsorbent and separated, obtain respectively the product gas of different component and/or concentration content.Only be with the difference of conventional pressure-swing absorption process, what adopt due to the above-mentioned absorbing unit device of the present invention is the structure of the serially connected master-secondary adsorption tower that can be communicated with or be ended by sequencing valve control, therefore, on the operating process basis that all (is equivalent to the adsorption tower structure of traditional structure form) under connected state at each master-secondary adsorption tower, further increased and can make absorbing unit operate in master-secondary adsorption tower all under cut-off state, to carry out respectively.Particularly in pressure equalizing, a part is all pressed and can under lead-secondary adsorption tower connected state, be carried out, and another part is all pressed and can be carried out, can make all to press more multi-selection and the flexibility carried out by different way, to adapt to and to meet the demand to different pressure-variable adsorption separating effects under cut-off state.For example, a kind of typical pressure-variable adsorption unit operation process and mode can be as following:
A. absorption: mist is sent into the each adsorption tower in connected state in absorbing unit device by the raw material gas inlet of main adsorption tower and adsorbed, gas vent by the secondary adsorption tower of end obtains the difficult absorbed component gas products of required purity or drops a hint, and adsorption process finishes;
B. drop pressure: after absorption finishes, each adsorption tower in be communicated with or cut-off state under carry out forward drop pressure, and by the gas vent of its secondary adsorption tower simultaneously from another secondary tower exit in absorbing unit device in boost pressure process carry out reverse boost pressure;
C. desorb: after drop pressure finishes, at each adsorption tower of this absorbing unit device under cut-off state, after main adsorption tower and the desorb of secondary adsorption tower difference, stripping gas is sent by the outlet of each adsorption tower, obtains the easy absorbed component gas products of desired concn content or drop a hint after main adsorption tower desorb; After secondary adsorption tower desorb, by the first secondary adsorption tower, to end pair adsorption tower, obtained respectively the component gas product that adsorption capacity successively decreases successively or drop a hint, desorption process finishes;
D. boost pressure: after desorption process finishes, in this absorbing unit device, each adsorption tower is under connection or cut-off state, through the outlet of its secondary adsorption tower, by in another absorbing unit device of above-mentioned c step drop pressure process, it being carried out, after reverse boost pressure, entering in a manner described next cyclic process.
After above-mentioned c step desorption process, the stripping gas being obtained by secondary adsorption tower except the gas product of the forms such as the specific components as collecting as required and/or composition, content, can also merge with unstripped gas after pressurization, re-starts adsorption treatment.
On above-mentioned basic operation process basis, according to actual production to the purity of gas products and/or the different situations of yield and the requirement that separate and/or obtain, on the one hand can be by the quantity of said psa unit device in adjustment System, and/or as above-mentioned by changing or being adjusted in different psa unit devices by connection or cut-off between each adsorption tower of sequencing valve control, and the conducting to said each corresponding gas branch path or cut-off by corresponding sequencing valve, change or adjust and above-mentionedly between different absorbing unit devices and/or different adsorption tower, combine about unit operations and process, reach the accommodation that increases and expand system, reach desirable separating effect and requirement and the object of raising gas product quality.
For example, after above-mentioned a step adsorption process finishes, the operation of the drop pressure of carrying out with other absorbing unit device that need carry out boost pressure, can adopt respectively following combination to carry out as required:
Mode one, main adsorption tower and each secondary adsorption tower in be communicated with or cut-off state under, between major and minor adsorption tower, take main adsorption tower as forward, secondary adsorption tower is as reverse mode, other is carried out making corresponding main adsorption tower in the absorbing unit device of boost pressure is that reverse, secondary adsorption tower is boost pressure forward;
Mode two, at main adsorption tower and each secondary adsorption tower, respectively all under cut-off state, and another carries out, between the corresponding adsorption tower of absorbing unit device of boost pressure, carrying out separately respectively boost pressure etc.
Above-mentioned different all pressures mode, can also be as required except can adopting separately, and the use that further mutually combines in a suitable manner, to reach desired effect and requirement.For example,, for reducing as the CO in Ammonia Production conversion gas
2pollution etc. easy absorbed component gas to secondary tower outlet, can adopt the equal press operation of above-mentioned different modes use in conjunction simultaneously, can reach and more be conducive to improve easy absorbed component gas product CO in Ammonia Production conversion gas
2purity, again can corresponding minimizing for the synthesis of ammonia, produce the effect of the difficult absorbed component degree of purifications such as hydrogen in conversion, nitrogen and the rate of recovery.
Test shows, adopt the above-mentioned psa unit device of the application, by the equal press operation mode of the difference between different adsorption towers and/or suitable combination in each absorbing unit device, when making the purity of the gas component that separates/obtain and/or the raising of yield have larger operating flexibility and accommodation, while particularly carrying out separation and purification for multicomponent form mist, another is also advantageous in that significantly, by the main adsorption tower of a set of pressure swing adsorption system and different secondary adsorption towers (while being provided with multistage secondary adsorption tower), can separate as required to produce simultaneously and obtain one, the gas product of two or more, and/or the component gas product of variable concentrations content.
Still, with the example that is separated into of Ammonia Production conversion gas, the adsorption process walking by above-mentioned a, can obtain meeting the difficult absorbed component gas of hydrogen, nitrogen etc. for the Ammonia Production product that required degree of purity requires by the exit of the secondary adsorption tower of final stage; After the king-tower desorb walking by c, can obtain the urea synthesis CO of desired concn
2etc. easy absorbed component gas product; And after the equal press operation of b step, each adsorption tower in be communicated with or cut-off state under desorb (vacuumizing), can be respectively by the gas branch path place of main adsorption tower upper end and secondary adsorption tower lower end obtain except above-mentioned difficult absorbed component and easily one or more other component gas products absorbed component gas product (as the CH in Ammonia Production conversion gas
4or the gas such as CO), or obtain take a certain gas component as main blending ingredients gas products.To wherein separating rear unwanted component gas, can continue to be fed into according to actual conditions processing or the emptying of next circulation.
On the other hand, on the basis of above-mentioned pressure-variable adsorption unit operation process, equally also can be according to the mode of operation of current conventional pressure-variable adsorption, corresponding increase according to actual needs or adjust some operating procedure.For example, while carrying out desorb operation, at each adsorption tower, under connection or cut-off state, can increase again in the usual way along putting the operations such as (forward emptying) or inverse put (reverse emptying).Wherein, adopt suitable putting while operating, the easy absorbed component gas product concentration obtaining is high, and in gas product, does not contain too much impurity (as H
2o and sulfide etc.), for example by above-mentioned synthetic-ammonia transformation gas, separate the CO obtaining
2when gas product is not only produced for urea, soda ash without desulfurization, even if make industrial carbon dioxide or carbon dioxide for foodstuff also without steps such as desulfurization and drying and dehydrating purifications; While adopting inverse put operation, though can contain some as H in the easy adsorption production gas obtaining
2the impurity such as O and sulfide, but it can be conducive to adsorbent reactivation.Concrete selection to additional operations and increasing/delete, by concrete condition, be determined with needing.
And for example, at said main adsorption tower, carry out emptying desorb, particularly adopt after forward emptying desorb, also can coordinate again as required the operation of the reverse desorb of finding time, so that the regeneration of adsorbent is more thorough, can also improve the concentration of gas treatment amount and desorption gas, obtain the easy absorbed component gas (as carbon dioxide) of higher concentration simultaneously.And the desorb of finding time can reduce investment outlay, but need many power consumptions, can determine whether adopt the desorb of finding time according to complex art economic evaluation, and/or the operational depth of the desorb of finding time.
Compared with two sections of aforementioned documents report or syllogic pressure swing absorption process, due to the desorb of absorbing unit device of the present invention after pressure equalizing finishes, be to carry out respectively under the isolation in cut-off at each adsorption tower.Therefore when main adsorption tower desorb, no matter whether secondary adsorption tower carries out independent desorb or does not carry out desorb and in wait state, all not emptying of available gas in secondary adsorption tower, can be used in a suitable manner all press, and it separately arranges intermediate buffer tank to reclaim these available gas compositions without need as said in document.Therefore, the pressure swing absorption process of master-secondary tower combined type absorbing unit device of the present invention not only can have advantages of that two sections of aforementioned documents (or three sections) formula pressure swing adsorption method has completely, can also save intermediate buffer tank and large quantities of expensive sequencing valve, thereby can make equipment investment save 10～20% simultaneously.Because the each adsorption tower in absorbing unit device of the present invention is not two to overlap the pressure swing adsorption system of independent operating separately in pressure-swing absorption process, only this also can make required floor space save 10～20%, and the connected state of each adsorption tower also more meets mass transfer and the desorb feature of pressure-variable adsorption, be conducive to sorption and desorption.
Table 1 adopts the each performance assessment criteria of pressure-changeable adsorption decarbonization device of this main and auxiliary tower technology
With the obvious advantage described in the more above-mentioned Granted publication CN100493671C of all technical of the present invention patent.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of the pressure swing adsorption system of a kind of psa unit device of the present invention.
Fig. 2 is the schematic diagram of the pressure swing adsorption system of the another kind of psa unit device of the present invention.
Fig. 3 is the pressure-variable adsorption operational system structural representation that embodiment 3 synthetic-ammonia transformation gas are separated.
Fig. 4 is the main adsorption tower operation sequential chart in each psa unit device of system shown in Figure 3.
Fig. 5 is the secondary adsorption tower operation sequential chart in each psa unit device of system shown in Figure 3
Fig. 6 is embodiment 4 pressure-variable adsorption operational system structural representations.
Fig. 7 is the main adsorption tower operation sequential chart in each psa unit device of system shown in Figure 6.
Fig. 8 is the secondary adsorption tower operation sequential chart in each psa unit device of system shown in Figure 6.
Fig. 9 is the ton ammonia integrated operation expense comparison (take coal as example) of the inventive method and two-period form method.
In figure: the outlet of gas after the secondary adsorption tower of tributary circuit, 5-between the main sequencing valve of tributary circuit, 3-, the import of 4-adsorption tower and main sequencing valve between the main adsorption tower of 1-, the outlet of 2-adsorption tower and main sequencing valve, 6-raw material gas inlet pipe, 10-process.
The specific embodiment
Below in conjunction with accompanying drawing 1-8, foregoing of the present invention is described in further detail again.But this should be interpreted as to the scope of the above-mentioned theme of the present invention only limits to following example.Without departing from the idea case in the present invention described above, various replacements or the change according to ordinary skill knowledge and customary means, made, all should comprise within the scope of the invention.
Fig. 1 is the pressure swing adsorption system with the psa unit installation composition of a kind of version of the present invention, and what in figure, represent in a schematic way is comprised of two psa unit device A, B arranged side by side.Two absorbing unit devices are all respectively a main adsorption tower 1 and secondary adsorption tower A1 of secondary adsorption tower 5(king-tower A-who sets gradually with head and the tail connected mode, the secondary adsorption tower B1 of king-tower B-) composite construction of composition, between end to end two adsorption towers, be provided with the sequencing valve 3 of break-make between control tower, the initial position of main adsorption tower 1 is provided with raw material gas inlet, and the afterbody of secondary adsorption tower is provided with gas vent 10 after treatment.Between the outlet of each adsorption tower and its adjacent sequencing valve 3, be provided with the tributary circuit 2 of at least one (shown in figure is two) with sequencing valve; Between the import of each adsorption tower and its adjacent sequencing valve 3, be also provided with the tributary circuit 4 of at least one (shown in figure is two) with sequencing valve.
Fig. 2 is the pressure swing adsorption system with the psa unit installation composition of the another kind of version of the present invention, is being comprised of two psa unit device A, B arranged side by side of representing in a schematic way in figure equally.With the difference of embodiment 1 be that two absorbing unit devices are all respectively a main adsorption tower 1 and two the secondary adsorption towers 5 that set gradually with head and the tail connected mode, the secondary adsorption tower A2 of the secondary adsorption tower A1-second of 52(king-tower A-first, the secondary adsorption tower B2 of the secondary adsorption tower B1-second of king-tower B-first) composite construction of composition.Except pressing with embodiment 1 same way at main adsorption tower 1(A1, B1) and the first secondary adsorption tower 5(A2, B2) between, be provided with outside the tributary circuit 2 of break-make sequencing valve 3 and front and back end thereof, at end to end two secondary adsorption tower (A1-A2, B1-B2) between, be also respectively equipped with break-make sequencing valve 32, and in its front and back end, be also respectively equipped with at least one (being two shown in figure) with the tributary circuit 22,42 of sequencing valve.
To take synthetic-ammonia transformation gas as unstripped gas (or synthetic-ammonia transformation gas) take coal, natural gas, wet goods as raw material, carry out pressure-variable adsorption separation.The composition of this routine synthetic-ammonia transformation gas is as shown in table 2:
The composition of table 2 synthetic-ammonia transformation gas
| Component | H 2 | N 2 | CO 2 | CO | CH 4 | O 2+Ar | Total sulfur | Water (vapour) |
| Concentration (%) | 52～53 | 17～18 | 17～28 | 1～6 | 1～2 | ≤0.8 | 150mg/Nm 3 | Saturated |
As shown in Figure 3, by 16 psa unit devices (A-A1)～(P-P1) form, each absorbing unit device is all with the composite construction being comprised of a main adsorption tower (A～P) and a secondary adsorption tower (A1～P1) shown in Fig. 1 for pressure swing adsorption system.In main adsorption tower, the adsorbent of filling is followed successively by activated alumina, activated carbon and/or Kiselgel A from down to up, and in secondary adsorption tower, the adsorbent of filling is activated carbon and/or Kiselgel A.The program of finding time that pressure swing adsorption system operation adopts two adsorption systems, ten once all to press.P1, P2 are that main adsorption tower solution smokes vavuum pump, and P3, P4 are that secondary adsorption tower solution smokes vavuum pump, and P5 is recycle gas compressor, V1 is inverse put carbon dioxide gas surge tank, V2 is carbon dioxide gas surge tank, and V3 is the carbon dioxide gas surge tank of finding time, and V4 is circulating air surge tank.The carbon dioxide stripping gas concentration of the present embodiment can reach 98.5%(V) more than, for the synthesis of urea, in the hydrogen of upper end outlet, nitrogen, carbon dioxide content concentration is less than 0.2%(V), to meet the needs of next step operation of synthetic ammonia.
Adsorption temp :≤40 ℃; Adsorptive pressure: 1.6Mpa (G), the discharge pressure of product carbon dioxide: 0.03Mpa (G).
Conversion gas enters after the main adsorption tower of pressure-swing absorption apparatus in adsorption step, adsorbent in adsorption tower optionally adsorbs water, organic sulfur, inorganic sulfur and the carbon dioxide component in conversion gas successively, the components such as the partial CO 2 not adsorbing and the difficult carbon monoxide adsorbing, methane, nitrogen, hydrogen enter the secondary adsorption tower of this absorbing unit from the main adsorption tower port of export, carbon dioxide is further adsorbed to component workshop sections from the secondary adsorption tower port of export enters such as the difficult carbon monoxide adsorbing, methane, nitrogen, hydrogen.A main adsorption tower of this pressure-swing absorption apparatus experiences successively in a cycle period: absorption (A), one all falls (E1D), two all fall (E2D), three all fall (E3D), four all fall (E4D), five all fall (E5D), six all fall (E6D), seven all fall (E7D), eight all fall (E8D), nine all fall (E9D), ten all fall (E10D), 11 all fall (E11D), inverse put (BD), (VC) finds time, 11 all rise (E11R), ten all rise (E10R), nine all rise (E9R), eight all rise (E8R), seven all rise (E7R), six all rise (E6R), five all rise (E5R), four all rise (E4R), three all rise (E3R), two all rise (E2R), one all rises (E1R), the steps such as (FR) of finally boosting, the secondary adsorption tower of this pressure-swing absorption apparatus experiences successively in a cycle period: absorption (A), one all falls (E1D), two all fall (E2D), three all fall (E3D), four all fall (E4D), five all fall (E5D), six all fall (E6D), seven all fall (E7D), eight all fall (E8D), nine all fall (E9D), ten all fall (E10D), 11 all fall (E11D), inverse put (BD), (VC) finds time, 11 all rise (E11R), ten all rise (E10R), nine all rise (E9R), eight all rise (E8R), seven all rise (E7R), six all rise (E6R), five all rise (E5R), four all rise (E4R), three all rise (E3R), two all rise (E2R), one all rises (E1R), the steps such as (FR) of finally boosting.Main adsorption tower in each psa unit device and the operation sequential of secondary adsorption tower are respectively as shown in Figure 4 and Figure 5.Now, take the first psa unit device A-A1 as example, the operating process of each adsorption tower in a circulation in adsorbent equipment is described.
(1) absorption A:
Now the first absorbing unit A-A1 has completed the FR step of finally boosting, open sequencing valve 1A, 2A, 11A, conversion gas enters the first absorbing unit A-A1 through G13 pipeline, in adsorption tower A, adsorbent optionally adsorbs the water in conversion gas successively, organic sulfur, inorganic sulfur and carbon dioxide component, the not carbon monoxide of the partial CO 2 of absorption and difficult absorption, methane, nitrogen, the components such as hydrogen enter secondary adsorption tower from the main adsorption tower port of export through sequencing valve 11A, carbon dioxide is further adsorbed, be difficult for the carbon monoxide of absorption, methane, nitrogen, the components such as hydrogen are from secondary adsorption tower port of export workshop section after sequencing valve 2A enters.As time goes on, the total amount of adsorbent water, organic sulfur, inorganic sulfur and carbon dioxide component constantly increases, and when the secondary adsorption tower port of export carbon dioxide component content of absorbing unit approaches 0.2%, stops air inlet, now absorption finishes, and closes sequencing valve 1A, 2A.
(2) drop pressure step for the first time, is called for short one and all falls E1D
After absorption finishes, close sequencing valve 1A, 2A, open sequencing valve 3A, 3J, 11J, gas in A-A1 absorbing unit enters J-J1 absorbing unit through G2 pipeline J-J1 absorbing unit is carried out to boost pressure (abbreviation: E1R) one time, when absorbing unit A-A1 and J-J1 pressure in a basic balance after, close sequencing valve 3A, 3J, 11J.
(3) drop pressure step for the second time, is called for short two and all falls E2D
One all falls after E1D finishes, open sequencing valve 4A, 4C, 11C, gas in A-A1 absorbing unit enters C-C1 absorbing unit through G3 pipeline C-C1 absorbing unit is carried out to secondary boost pressure (abbreviation: E2R), when absorbing unit A-A1 and C-C1 pressure in a basic balance after, close sequencing valve 4C, 11C.
(4) drop pressure step for the third time, is called for short three and all falls E3D
Two all fall after E2D finishes, open sequencing valve 4K, 11K, gas in A-A1 absorbing unit enters K-K1 absorbing unit through G3 pipeline K-K1 absorbing unit is carried out to boost pressures (abbreviation: E3R) three times, when absorbing unit A-A1 and K-K1 pressure in a basic balance after, close sequencing valve 4A, 4K, 11K.
(5) the 4th drop pressure steps, are called for short four and all fall E4D
Three all fall after E3D finishes, open sequencing valve 5A, 5D, 11D, gas in A-A1 absorbing unit enters D-D1 absorbing unit through G4 pipeline D-D1 absorbing unit is carried out to boost pressures (abbreviation: E4R) four times, when absorbing unit A-A1 and D-D1 pressure in a basic balance after, close sequencing valve 5D, 11D.
(6) the 5th drop pressure steps, are called for short five and all fall E5D
Four all fall after E4D finishes, open sequencing valve 5L, 11L, gas in A-A1 absorbing unit enters L-L1 absorbing unit through G4 pipeline L-L1 absorbing unit is carried out to boost pressures (abbreviation: E5R) five times, when absorbing unit A-A1 and L-L1 pressure in a basic balance after, close sequencing valve 5A, 5L, 11L.
(7) the 6th drop pressure steps, are called for short six and all fall E6D
Five all fall after E5D finishes, open sequencing valve 6A, 6E, 11E, gas in A-A1 absorbing unit enters E-E1 absorbing unit through G5 pipeline E-E1 absorbing unit is carried out to boost pressures (abbreviation: E6R) six times, when absorbing unit A-A1 and E-E1 pressure in a basic balance after, close sequencing valve 6E, 11E.
(8) the 7th drop pressure steps, are called for short seven and all fall E7D
Six all fall after E6D finishes, open sequencing valve 6M, 11M, gas in A-A1 absorbing unit enters M-M1 absorbing unit through G5 pipeline M-M1 absorbing unit is carried out to boost pressures (abbreviation: E7R) seven times, when absorbing unit A-A1 and M-M1 pressure in a basic balance after, close sequencing valve 6A, 6M, 11M.
(9) the 8th drop pressure steps, are called for short eight and all fall E8D
Seven all fall after E7D finishes, open sequencing valve 7A, 7F, 11F, gas in A-A1 absorbing unit enters F-F1 absorbing unit through G6 pipeline F-F1 absorbing unit is carried out to boost pressures (abbreviation: E8R) eight times, when absorbing unit A-A1 and F-F1 pressure in a basic balance after, close sequencing valve 7F, 11F.
(10) the 9th drop pressure steps, are called for short nine and all fall E9D
Eight all fall after E8D finishes, open sequencing valve 7N, 11N, gas in A-A1 absorbing unit enters N-N1 absorbing unit through G6 pipeline N-N1 absorbing unit is carried out to boost pressures (abbreviation: E9R) nine times, when absorbing unit A-A1 and N-N1 pressure in a basic balance after, close sequencing valve 7A, 7N, 11N.
(11) the tenth drop pressure steps, are called for short ten and all fall E10D
Nine all fall after E9D finishes, open sequencing valve 8A, 8G, 11G, gas in A-A1 absorbing unit enters G-G1 absorbing unit through G7 pipeline G-G1 absorbing unit is carried out to boost pressures (abbreviation: E10R) ten times, when absorbing unit A-A1 and G-G1 pressure in a basic balance after, close sequencing valve 8G, 11G.
(12) the ten drop pressure steps, are called for short 11 and all fall E11D
Ten all fall after E10D finishes, open sequencing valve 8O, 11O, gas in A-A1 absorbing unit enters O-O1 absorbing unit through G7 pipeline O-O1 absorbing unit is carried out to boost pressures (abbreviation: E11R) 11 times, when absorbing unit A-A1 and O-O1 pressure in a basic balance after, close sequencing valve 8A, 11A, 8O, 11O.
(13) main adsorption tower and secondary adsorption tower inverse put depressurization step, is called for short BD
11 all fall after E11D finishes, open sequencing valve 9A, 12A, 20, gas in main adsorption tower A enters inverse put gas surge tank V1 through G11 pipeline, when main adsorption tower A and V1 pressure in a basic balance after, close sequencing valve 20, open sequencing valve 30, remaining gas is sent into hypomere operation through pipeline G15, when the pressure in main adsorption tower A and back segment operation inlet pressure are closed sequencing valve 12A, 30 after in a basic balance; Gas in secondary adsorption tower A1 to circulating air surge tank V4, after the gas pressure in the gas in secondary adsorption tower A1 and circulating air surge tank V4 is in a basic balance, is closed sequencing valve 9A through G8 pipeline inverse put.
(14) main adsorption tower and secondary adsorption tower pumpdown step, is called for short VC
After main adsorption tower, secondary adsorption tower inverse put finish, open sequencing valve 10A, 13A, the gas in main adsorption tower A is extracted out and is entered surge tank V3 by vavuum pump P1 through G14 pipeline, then delivers to next workshop section.Gas in secondary adsorption tower A1 is extracted out and is entered circulating air surge tank V4 by vavuum pump P3 through G10 pipeline, and the gas in circulating air surge tank V4 is sent into unstripped gas pipeline G13 through G16 pipeline after recycle compressor P5 pressurization, remakes absorption again.When drop to approximately-0.07MPa of gas pressure in main adsorption tower and secondary adsorption tower, close sequencing valve 10A, 13A.
(15) the tenth steps of once boosting, are called for short 11 and all rise E11R
After main adsorption tower, secondary adsorption tower pumpdown step finish, open sequencing valve 8A, 11A, 8J, 11J, gas in absorbing unit J-J1 enters absorbing unit A-A1 through G7 pipeline, to absorbing unit A-A1 carry out the tenth once reverse boost pressure (be called for short: E11R), when absorbing unit A-A1 and absorbing unit J-J1 pressure in a basic balance after, close sequencing valve 8J, 11J.
(16) the tenth boost pressure steps, are called for short ten and all rise E10R
The tenth once boosts after step finishes, open sequencing valve 8C, 10C, gas in absorbing unit C-C1 enters absorbing unit A-A1 through G7 pipeline, absorbing unit A-A1 is carried out to the tenth reverse boost pressure (to be called for short: E10R), when absorbing unit A-A1 and absorbing unit C-C1 pressure in a basic balance after, close sequencing valve 8A, 8C, 11C.
(17) the 9th boost pressure steps, are called for short nine and all rise E9R
After all rising E10R the tenth time and finishing, open sequencing valve 7A, 7K, 11K, gas in absorbing unit K-K1 enters absorbing unit A-A1 through G6 pipeline, absorbing unit A-A1 is carried out to the 9th reverse boost pressure (to be called for short: E9R), when absorbing unit A-A1 and absorbing unit K-K1 pressure in a basic balance after, close sequencing valve 7K, 11K.
(18) the 8th boost pressure steps, are called for short eight and all rise E8R
After all rising E9R the 9th time and finishing, open sequencing valve 7D, 11D, gas in absorbing unit D-D1 enters absorbing unit A-A1 through G6 pipeline, absorbing unit A-A1 is carried out to the 8th reverse boost pressure (to be called for short: E8R), when absorbing unit A-A1 and absorbing unit D-D1 pressure in a basic balance after, close sequencing valve 7A, 7D, 11D.
(19) the 7th boost pressure steps, are called for short seven and all rise E7R
After all rising E8R the 8th time and finishing, open sequencing valve 6A, 6L, 11L, gas in L-L1 absorbing unit enters A-A1 absorbing unit through G5 pipeline absorbing unit A-A1 is carried out to reverse boost pressure (abbreviation: E7R) the 8th time, when absorbing unit A-A1 and L-L1 pressure in a basic balance after, close sequencing valve 6L, 11L.
(20) the 6th boost pressure steps, are called for short six and all rise E6R
After all rising E7R the 7th time and finishing, open sequencing valve 6E, 11E, gas in E-E1 absorbing unit enters A-A1 absorbing unit through G5 pipeline A-A1 absorbing unit is carried out to boost pressures (abbreviation: E6R) six times, when absorbing unit A-A1 and E-E1 pressure in a basic balance after, close sequencing valve 6A, 6E, 11E.
(21) the 5th boost pressure steps, are called for short five and all rise E5R
After all rising E6R the 6th time and finishing, open sequencing valve 5A, 5M, 11M, gas in M-M1 absorbing unit enters A-A1 absorbing unit through G4 pipeline A-A1 absorbing unit is carried out to boost pressures (abbreviation: E5R) five times, when absorbing unit A-A1 and M-M1 pressure in a basic balance after, close sequencing valve 5M, 11M.
(22) the 4th boost pressure steps, are called for short four and all rise E4R
After all rising E5R the 5th time and finishing, open sequencing valve 5F, 11F, gas in F-F1 absorbing unit enters A-A1 absorbing unit through G4 pipeline A-A1 absorbing unit is carried out to boost pressures (abbreviation: E4R) four times, when absorbing unit A-A1 and F-F1 pressure in a basic balance after, close sequencing valve 5A, 5F, 11F.
(23) boost pressure step for the third time, is called for short three and all rises E3R
After all rising E4R the 4th time and finishing, open sequencing valve 4A, 4N, 11N, gas in N-N1 absorbing unit enters A-A1 absorbing unit through G3 pipeline A-A1 absorbing unit is carried out to boost pressures (abbreviation: E3R) three times, when absorbing unit A-A1 and N-N1 pressure in a basic balance after, close sequencing valve 4N, 9N.
(24) boost pressure step for the second time, is called for short two and all rises E2R
After all rising for the third time E3R and finishing, open sequencing valve 4G, 11G, gas in G-G1 absorbing unit enters A-A1 absorbing unit through G3 pipeline A-A1 absorbing unit is carried out to secondary boost pressure (abbreviation: E2R), when absorbing unit A-A1 and G-G1 pressure in a basic balance after, close sequencing valve 4A, 4G, 11G.
(25) boost pressure step for the first time, is called for short one and all rises E1R
After all rising for the second time E2R and finishing, open sequencing valve 3A, 3O, 11O, gas in O-O1 absorbing unit enters A-A1 absorbing unit through G2 pipeline A-A1 absorbing unit is carried out to boost pressure (abbreviation: E1R) one time, when absorbing unit A-A1 and O-O1 pressure in a basic balance after, close sequencing valve 3O, 11O.
(26) FR that finally boosts
After boost pressure finishes for the first time, open sequencing valve 10, utilize and work off one's feeling vent one's spleen and through G2 pipeline, absorbing unit A-A1 is boosted in the absorbing unit of absorption phase, when absorbing unit A-A1 pressure rises to while approaching adsorptive pressure, close sequencing valve 3A, 11A, 10.
So far, A-A1 absorbing unit has completed a circulation.All the other B-B1～P-P1 psa unit devices are the same with the circulation step of A-A1 absorbing unit device, on the time, are just mutually to stagger, and have two absorbing units in absorption phase in each time period simultaneously.
The ton ammonia integrated operation expense comparison (take coal as raw material) of the above-mentioned pressure swing absorption process of the present invention and conventional two-period form pressure swing absorption process as shown in Figure 9.
To take synthetic-ammonia transformation gas as unstripped gas (or synthetic-ammonia transformation gas) take coal, natural gas, wet goods as raw material, carry out pressure-variable adsorption separation.The composition of this routine synthetic-ammonia transformation gas is as shown in table 3:
The composition of table 3 synthetic-ammonia transformation gas
| Component | H 2 | N 2 | CO 2 | CO | CH 4 | O 2+Ar | Total sulfur | Water (vapour) |
| Concentration (%) | 52～53 | 17～18 | 17～28 | 1～6 | 1～2 | ≤0.8 | 150mg/Nm 3 | Saturated |
As shown in Figure 6, by 16 psa unit devices (A-A1)～(P-P1) form, each absorbing unit device is all with the composite construction being comprised of a main adsorption tower (A～P) and a secondary adsorption tower (A1～P1) shown in Fig. 1 for pressure swing adsorption system.In main adsorption tower, the adsorbent of filling is followed successively by activated alumina, activated carbon and/or Kiselgel A from down to up, and in secondary adsorption tower, the adsorbent of filling is activated carbon and/or Kiselgel A.The program of finding time that pressure swing adsorption system operation adopts two adsorption systems, all presses for 7 times.P1, P2, P3, P4 are that main adsorption tower solution smokes vavuum pump, and P5, P6, P7, P8 are that secondary adsorption tower solution smokes vavuum pump.The carbon dioxide stripping gas concentration of the present embodiment can reach 98.5%(V) more than, for the synthesis of urea, in the hydrogen of upper end outlet, nitrogen, carbon dioxide content concentration is less than 0.2%(V), to meet the needs of next step operation of synthetic ammonia.
Adsorption temp :≤40 ℃; Adsorptive pressure: 1.2Mpa (G), the discharge pressure of product carbon dioxide: 0.03Mpa (G).
Conversion gas enters after the main adsorption tower of pressure-swing absorption apparatus in adsorption step, adsorbent in adsorption tower optionally adsorbs water, organic sulfur, inorganic sulfur and the carbon dioxide component in conversion gas successively, the components such as the partial CO 2 not adsorbing and the difficult carbon monoxide adsorbing, methane, nitrogen, hydrogen enter the secondary adsorption tower of this absorbing unit from the main adsorption tower port of export, carbon dioxide is further adsorbed to component workshop sections from the secondary adsorption tower port of export enters such as the difficult carbon monoxide adsorbing, methane, nitrogen, hydrogen.A main adsorption tower of this pressure-swing absorption apparatus experiences successively in a cycle period: absorption (A), one all falls (E1D), two all fall (E2D), three all fall (E3D), four all fall (E4D), five all fall (E5D), six all fall (E6D), seven all fall (E7D), inverse put (BD), (VC) finds time, seven all rise (E7R), six all rise (E6R), five all rise (E5R), four all rise (E4R), three all rise (E3R), two all rise (E2R), one all rises (E1R), the steps such as (FR) of finally boosting, the secondary adsorption tower of this pressure-swing absorption apparatus experiences successively in a cycle period: absorption (A), one all falls (E1D), two all fall (E2D), three all fall (E3D), four all fall (E4D), five all fall (E5D), six all fall (E6D), seven all fall (E7D), along putting (PP), (VC) finds time, seven all rise (E7R), six all rise (E6R), five all rise (E5R), four all rise (E4R), three all rise (E3R), two all rise (E2R), one all rises (E1R), the steps such as (FR) of finally boosting.Main adsorption tower in each psa unit device and the operation sequential of secondary adsorption tower are respectively as shown in Figure 7 and Figure 8.Now, take the first psa unit device A-A1 as example, the operating process of each adsorption tower in a circulation in adsorbent equipment is described.
(1) absorption A:
Now the first absorbing unit A-A1 has completed the FR step of finally boosting, open sequencing valve 1A, 2A, 9A, conversion gas enters the first absorbing unit A-A1 through G10 pipeline, in adsorption tower A, adsorbent optionally adsorbs the water in conversion gas successively, organic sulfur, inorganic sulfur and carbon dioxide component, the not carbon monoxide of the partial CO 2 of absorption and difficult absorption, methane, nitrogen, the components such as hydrogen enter secondary adsorption tower from the main adsorption tower port of export through sequencing valve 9A, carbon dioxide is further adsorbed, be difficult for the carbon monoxide of absorption, methane, nitrogen, the components such as hydrogen are from secondary adsorption tower port of export workshop section after sequencing valve 2A enters.As time goes on, the total amount of adsorbent water, organic sulfur, inorganic sulfur and carbon dioxide component constantly increases, and when the secondary adsorption tower port of export carbon dioxide component content of absorbing unit approaches 0.2%, stops air inlet, now absorption finishes, and closes sequencing valve 1A, 2A.
(2) drop pressure step for the first time, is called for short one and all falls E1D
After absorption finishes, close sequencing valve 1A, 2A, open sequencing valve 3A, 3F (9F is in opening), gas in A-A1 absorbing unit enters F-F1 absorbing unit through G2 pipeline F-F1 absorbing unit is carried out to boost pressure (abbreviation: E1R) for the first time, when absorbing unit A-A1 and F-F1 pressure in a basic balance after, close sequencing valve 3A, 3F.
(3) drop pressure step for the second time, is called for short two and all falls E2D
One all falls after E1D finishes, open sequencing valve 4A, 4J(9J in opening), gas in A-A1 absorbing unit enters J-J1 absorbing unit through G3 pipeline J-J1 absorbing unit is carried out to boost pressure (abbreviation: E2R) for the second time, when absorbing unit A-A1 and J-J1 pressure in a basic balance after, close sequencing valve 4J.
(4) drop pressure step for the third time, is called for short three and all falls E3D
Two all fall after E2D finishes, open sequencing valve 4N (9N is in opening), gas in A-A1 absorbing unit enters N-N1 absorbing unit through G3 pipeline N-N1 absorbing unit is carried out to boost pressure (abbreviation: E3R) for the third time, when absorbing unit A-A1 and N-N1 pressure in a basic balance after, close sequencing valve 4A, 9A, 4N, 9N.
(5) the 4th drop pressure steps, are called for short four and all fall E4D
Three all fall after E3D finishes, open sequencing valve 5A, 10A, 5C, 10C (9A, 9C are all in closed condition), gas in secondary tower A1 enters secondary tower C1 through G4 pipeline secondary tower C1 is carried out to boost pressure the 4th time, gas in king-tower A enters king-tower C through G8 pipeline king-tower C is carried out to boost pressure the 4th time, (be called for short: E4R), when secondary tower A1 and secondary tower C1, king-tower A and king-tower C pressure in a basic balance after, close sequencing valve 5C, 10C.
(6) the 5th drop pressure steps, are called for short five and all fall E5D
Four all fall after E4D finishes, open sequencing valve 5G, 10G (9A, 9G are all in closed condition), gas in secondary tower A1 enters secondary tower G1 through G4 pipeline secondary tower G1 is carried out to boost pressure the 5th time, gas in king-tower A enters king-tower G through G8 pipeline king-tower G is carried out to boost pressure the 5th time, (be called for short: E4R), when secondary tower A1 and secondary tower G1, king-tower A and king-tower G pressure in a basic balance after, close sequencing valve 5A, 10A, 5G, 10G.
(7) the 6th drop pressure steps, are called for short six and all fall E6D
Five all fall after E5D finishes, open sequencing valve 6A, 11A, 6K, 11K (9A, 9K are all in closed condition), gas in secondary tower A1 enters secondary tower K1 through G5 pipeline secondary tower K1 is carried out to boost pressure the 6th time, gas in king-tower A enters king-tower K through G9 pipeline king-tower K is carried out to boost pressure the 6th time, (be called for short: E4R), when secondary tower A1 and secondary tower K1, king-tower A and king-tower K pressure in a basic balance after, close sequencing valve 6K, 11K.
(8) the 7th drop pressure steps, are called for short seven and all fall E7D
Six all fall after E6D finishes, open sequencing valve 6O, 11O (9A, 9O are all in closed condition), gas in secondary tower A1 enters secondary tower O1 through G5 pipeline secondary tower O1 is carried out to boost pressure the 7th time, gas in king-tower A enters king-tower O through G9 pipeline king-tower O is carried out to boost pressure the 7th time, (be called for short: E4R), when secondary tower A1 and secondary tower O1, king-tower A and king-tower O pressure in a basic balance after, close sequencing valve 6A, 11A, 6O, 11O.
(9) main adsorption tower and secondary adsorption tower, along inverse put depressurization step, are called for short BD
Seven all fall after E7D finishes, and open sequencing valve 7A, 9A, and the gas in king-tower A and secondary tower A1 enters inverse put gas surge tank V1 through G6 pipeline, when main adsorption tower A and V1 pressure in a basic balance after, close 7A, 9A.
(10) main adsorption tower and secondary adsorption tower pumpdown step, is called for short VC
Main adsorption tower, secondary adsorption tower are opened sequencing valve 8A, 12A after finishing along inverse put, and the gas in main adsorption tower A is extracted out and entered surge tank V2 by vavuum pump P1 through G11 pipeline, then delivers to next workshop section.Gas in secondary adsorption tower A1 is extracted out and is entered circulating air surge tank V3 by vavuum pump P5 through G7 pipeline, and in V3, gas is delivered to gas fired-boiler burning producing steam.When drop to approximately-0.07MPa of gas pressure in main adsorption tower and secondary adsorption tower, close sequencing valve 8A, 12A.
(11) the 7th boost pressure steps, are called for short seven and all rise E7R
After vacuumizing desorb and finishing, open sequencing valve 6A, 11A, 6F, 11F, (9A, 9F are all in closed condition), gas in secondary tower F1 enters secondary tower A1 through G5 pipeline secondary tower A1 is carried out to boost pressure seven times, gas in king-tower F enters king-tower A through G9 pipeline king-tower A is carried out to boost pressure seven times, (be called for short: E7R), when secondary tower A1 and secondary tower F1, king-tower A and king-tower F pressure in a basic balance after, close sequencing valve 6F, 11F.
(12) the 6th boost pressure steps, are called for short six and all rise E6R
After all rising E7R the 7th time and finishing, open sequencing valve 6J, 11J, (9A, 9J are all in closed condition), gas in secondary tower J1 enters secondary tower A1 through G5 pipeline secondary tower A1 is carried out to boost pressure six times, gas in king-tower J enters king-tower A through G9 pipeline king-tower A is carried out to boost pressure six times, (be called for short: E6R), when secondary tower A1 and secondary tower J1, king-tower A and king-tower J pressure in a basic balance after, close sequencing valve 6J, 11J.
(13) the 5th boost pressure steps, are called for short five and all rise E5R
After all rising E6R the 6th time and finishing, open sequencing valve 5A, 10A, 5N, 10N, (9A, 9N are all in closed condition), gas in secondary tower N1 enters secondary tower A1 through G4 pipeline secondary tower A1 is carried out to boost pressure five times, gas in king-tower N enters king-tower A through G8 pipeline king-tower A is carried out to boost pressure five times, (be called for short: E5R), when secondary tower A1 and secondary tower N1, king-tower A and king-tower N pressure in a basic balance after, close sequencing valve 5N, 10N.
(14) the 4th boost pressure steps, are called for short four and all rise E4R
After all rising E5R the 5th time and finishing, open sequencing valve 5C, 10C, (9A, 9C are all in closed condition), gas in secondary tower C1 enters secondary tower A1 through G4 pipeline secondary tower A1 is carried out to boost pressure four times, gas in king-tower C enters king-tower A through G8 pipeline king-tower A is carried out to boost pressure four times, (be called for short: E4R), when secondary tower A1 and secondary tower C1, king-tower A and king-tower C pressure in a basic balance after, close sequencing valve 5A, 10A, 5C, 10C.
(15) boost pressure step for the third time, is called for short three and all rises E3R
After all rising E4R the 4th time and finishing, open sequencing valve 4A, 9A, 4G, 9G, gas in G-G1 absorbing unit enters A-A1 absorbing unit through G3 pipeline A-A1 absorbing unit is carried out to boost pressures (abbreviation: E3R) three times, when absorbing unit A-A1 and N-N1 pressure in a basic balance after, close sequencing valve 4G.
(16) boost pressure step for the second time, is called for short two and all rises E2R
After all rising for the third time E3R and finishing, open sequencing valve 4K (9A, 9K are all in opening), gas in K-K1 absorbing unit enters A-A1 absorbing unit through G3 pipeline A-A1 absorbing unit is carried out to secondary boost pressure (abbreviation: E2R), when absorbing unit A-A1 and G-G1 pressure in a basic balance after, close sequencing valve 4A, 4K.
(17) boost pressure step for the first time, is called for short one and all rises E1R
After all rising for the second time E2R and finishing, open sequencing valve 3A, 3O (9A, 9O are all in opening), gas in O-O1 absorbing unit enters A-A1 absorbing unit through G2 pipeline A-A1 absorbing unit is carried out to boost pressure (abbreviation: E1R) one time, when absorbing unit A-A1 and O-O1 pressure in a basic balance after, close sequencing valve 3O, 11O.
(18) FR that finally boosts
After boost pressure finishes for the first time, open sequencing valve 10, utilize and work off one's feeling vent one's spleen and through G2 pipeline, absorbing unit A-A1 is boosted in the absorbing unit of absorption phase, when absorbing unit A-A1 pressure rises to while approaching adsorptive pressure, close sequencing valve 3A, 9A, 10.
So far, A-A1 absorbing unit has completed a circulation.All the other B-B1～P-P1 psa unit devices are the same with the circulation step of A-A1 absorbing unit device, on the time, are just mutually to stagger, and have two absorbing units in absorption phase in each time period simultaneously.
Although illustrated and described embodiments of the invention, for the ordinary skill in the art, be appreciated that without departing from the principles and spirit of the present invention and can carry out multiple variation, modification, replacement and modification to these embodiment, scope of the present invention is limited by claims and equivalent thereof.
Claims (7)
1. a psa unit device, is characterized in that: this device unit is comprised of a main adsorption tower (1) and one or more secondary adsorption tower (5); Between main adsorption tower (1) and secondary adsorption tower (5), join end to end; Between each end to end adsorption tower, be respectively equipped with the sequencing valve (3) of break-make between control tower, main adsorption tower (1) bottom is connected with raw material gas inlet pipe (6); The outlet (10) of gas after the secondary adsorption tower of final stage top is provided with and processes.
2. psa unit device as claimed in claim 1, is characterized in that: between main adsorption tower outlet and sequencing valve (3), be provided with one or more than one tributary circuits with sequencing valve (2).
3. psa unit device as claimed in claim 1, is characterized in that: between secondary adsorption tower import and sequencing valve (3), be provided with one or more than one tributary circuits with sequencing valve (4).
4. as right, want the psa unit device as described in 1-3 any one, it is characterized in that: the quantity of the secondary adsorption tower of each absorbing unit device is at least one, and the sequencing valve of controlling break-make is set respectively between end to end secondary tower.
5. a pressure swing adsorption system, it is characterized in that: in this pressure swing adsorption system, comprise two or more psa unit devices as described in claim 1-4 any one, each psa unit device connects in parallel, between them, by pipeline, connect, pipeline is provided with sequencing valve.
6. the method that utilization wants the pressure swing adsorption system as described in 5 to carry out the pressure-variable adsorption separation of mist as right, it is characterized in that: each absorbing unit with sequential interlace mode respectively in the following manner, make pending mist respectively through comprise absorption, all press and desorption process, be separated into easy absorbed component gas and difficult absorbed component gas:
A. absorption: mist is sent into the each adsorption tower in connected state in absorbing unit device by the raw material gas inlet of main adsorption tower (1) and adsorbed, gas outlet tube (10) by the secondary adsorption tower of end obtains the difficult absorbed component gas products of required purity or drops a hint, and adsorption process finishes;
B. drop pressure: after absorption finishes, each adsorption tower in be communicated with or cut-off state under carry out forward drop pressure, and by the gas outlet tube (9) of its secondary adsorption tower simultaneously from another secondary tower exit in absorbing unit device in boost pressure process carry out reverse boost pressure;
C. desorb: after drop pressure finishes, at each adsorption tower of this absorbing unit device under cut-off state, after main adsorption tower and the desorb of secondary adsorption tower difference, stripping gas is sent by the stripping gas pipeline of each adsorption tower, obtains the easy absorbed component gas products of desired concn content or drop a hint after main adsorption tower desorb; After secondary adsorption tower desorb, by the first secondary adsorption tower, to end pair adsorption tower, obtained respectively the component gas product that adsorption capacity successively decreases successively or drop a hint, desorption process finishes;
D. boost pressure: after desorption process finishes, in this absorbing unit device, each adsorption tower is under connection or cut-off state, through the outlet of its secondary adsorption tower, by in another absorbing unit device of above-mentioned C step drop pressure process, it being carried out, after reverse boost pressure, entering in a manner described next cyclic process.
7. the method that pressure-variable adsorption as claimed in claim 6 separates, is characterized in that: after c step desorption process, the stripping gas being obtained by secondary adsorption tower merges with unstripped gas after pressurization, re-starts adsorption treatment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310664545.8A CN103736361A (en) | 2013-12-10 | 2013-12-10 | Pressure swing adsorption unit device, pressure swing adsorption system and adsorption separation method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310664545.8A CN103736361A (en) | 2013-12-10 | 2013-12-10 | Pressure swing adsorption unit device, pressure swing adsorption system and adsorption separation method thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103736361A true CN103736361A (en) | 2014-04-23 |
Family
ID=50493468
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310664545.8A Pending CN103736361A (en) | 2013-12-10 | 2013-12-10 | Pressure swing adsorption unit device, pressure swing adsorption system and adsorption separation method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103736361A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105233624A (en) * | 2015-10-21 | 2016-01-13 | 中国石油化工股份有限公司 | Organic gas processing device based on adsorption under pressure and using method thereof |
| CN105600752A (en) * | 2016-03-29 | 2016-05-25 | 河北天善生物技术有限公司 | Method and system for purifying hydrogen gas in biomass gas |
| CN113041782A (en) * | 2021-03-15 | 2021-06-29 | 西南化工研究设计院有限公司 | Gas pressure swing adsorption separation and purification system and separation and purification method thereof |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1460535A (en) * | 2003-06-02 | 2003-12-10 | 王玉 | Directly-series-connected one-step pressure swing adsorption process |
| CN101249369A (en) * | 2008-04-07 | 2008-08-27 | 北京科技大学 | Method for multiple-unit coupled vacuum voltage transformation adsorption CO2 between segments |
-
2013
- 2013-12-10 CN CN201310664545.8A patent/CN103736361A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1460535A (en) * | 2003-06-02 | 2003-12-10 | 王玉 | Directly-series-connected one-step pressure swing adsorption process |
| CN101249369A (en) * | 2008-04-07 | 2008-08-27 | 北京科技大学 | Method for multiple-unit coupled vacuum voltage transformation adsorption CO2 between segments |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105233624A (en) * | 2015-10-21 | 2016-01-13 | 中国石油化工股份有限公司 | Organic gas processing device based on adsorption under pressure and using method thereof |
| CN105600752A (en) * | 2016-03-29 | 2016-05-25 | 河北天善生物技术有限公司 | Method and system for purifying hydrogen gas in biomass gas |
| CN105600752B (en) * | 2016-03-29 | 2018-04-17 | 河北天善生物技术有限公司 | A kind of method of purification and its system for being used for hydrogen in biological fuel gas |
| CN113041782A (en) * | 2021-03-15 | 2021-06-29 | 西南化工研究设计院有限公司 | Gas pressure swing adsorption separation and purification system and separation and purification method thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106693608B (en) | A kind of process for separating and recovering of oil refinery dry gas | |
| JP4579983B2 (en) | Gas separation method by two-stage full recovery transformer adsorption | |
| CN102245500B (en) | Production of hydrogen from a reforming gas and simultaneous capture of CO2 co-product | |
| CN101978235B (en) | Method and apparatus for separating blast furnace gas | |
| CN103585856A (en) | Multi-backflow pressure swing adsorption method | |
| CN101108295B (en) | Method of removing CO2 from switch gas by pressure swing adsorption with replacing and recycling step | |
| CN101249370B (en) | Voltage transformation adsorption method for circulation valuable gas | |
| CN103787285B (en) | Five tower swing adsorption nitrogen producing apparatus | |
| CN103357245A (en) | Adsorption process | |
| CN112678773B (en) | Process for producing hydrogen and coproducing LNG (liquefied Natural gas) by using raw gas | |
| CN104986735B (en) | A kind of method for improving hydrogen recovery rate | |
| CN103736361A (en) | Pressure swing adsorption unit device, pressure swing adsorption system and adsorption separation method thereof | |
| CN102580457A (en) | Oxygen generating device special for ozone device | |
| CN105347304B (en) | A kind of double high desorption PSA with pressure carry hydrogen methods | |
| CN106413851A (en) | Gas-condensing method | |
| CN100444933C (en) | Pressure-changing adsorption method for recovering low-partial-pressure gas | |
| CN102500190B (en) | A kind of cleaning and recovering process for enriched gas source | |
| CN101531342B (en) | Device and method for producing oxygen by means of pressure swing adsorption (PSA) by five beds | |
| CN103695063A (en) | Method for concentrating low-concentration methane gas | |
| CN203663664U (en) | Device for separating and recovering hydrocarboncomponents and hydrogen from refinery dry gas | |
| CN102091501A (en) | Upper and lower pressure-equalizing pressure swing adsorption method | |
| CN102600699B (en) | Pressure-variable adsorption gas separation device | |
| CN202519026U (en) | Special oxygen generating device for ozone generator | |
| CN100469686C (en) | Method and equipment for separating oxygen from air | |
| CN103223288A (en) | Pressure swing adsorption decarbonization device and process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20140423 |