CN102343196A - Method and device for one-stage pressure swing adsorption hydrogen extraction and carbon-rich gas recovery - Google Patents
Method and device for one-stage pressure swing adsorption hydrogen extraction and carbon-rich gas recovery Download PDFInfo
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Abstract
The invention discloses a method and a device for one-stage pressure swing adsorption hydrogen extraction and carbon-rich gas recovery. The method adopts a pressure swing adsorption principle. Through the method and the device, high-purity hydrogen is extracted from methanol synthesis discharge gas and is utilized as product gas; simultaneously, high-purity carbon-rich gas produced in recovery desorption is utilized as feed gas utilized for a methanol device; produced concurrently discharged hydrogen with high concentration is fed back to a methanol system; and produced concurrently discharged replacement gas with low concentration is utilized as fuel gas and is discharged into a fuel pipe net. Each one cycle of the method comprises a adsorption process, a concurrent discharge process, a displacement process, a countercurrent discharge process, a vacuum-pumping process, a even pressure rise process and a final stroke process. Compared with a conventional two-stage method-based hydrogen extraction technology, the method provided by the invention improves a total hydrogen recovery rate and a product hydrogen recovery rate of the device. Through the method and the device, high-purity carbon-rich gas can be extracted from analysis gas. The device has the advantages of low cost, small floor space and good economic benefits.
Description
Technical field
The present invention relates to a kind of transformation absorption device for producing hydrogen, refer more particularly to method and device that a kind of one-stage process transformation absorption that can greatly improve rich carbon gas recovery rate is carried hydrogen and reclaimed rich carbon gas.
Background technology
Transform to coke-stove gas in the similar device of system methyl alcohol or coproducing synthetic ammonia (or needing hydrogen production); Contain hydrogen in the unstripped gas; Carbon dioxide; Carbon monoxide; Gas componants such as nitrogen; The general two-phase method hydrogen production process that adopts; Promptly earlier unstripped gas is obtained raw hydrogen through the pressure swing adsorption decarbonization flow processing; The carbonaceous gas that parses in the decarburization flow process (rich carbon gas) returns the methyl alcohol system; Again raw hydrogen is carried the finished hydrogen that the hydrogen flow processing obtains higher degree through the absorption of molecular sieve transformation; Carry the gas that parses in the hydrogen flow process and directly send to fuel pipe network or emptying; Like Chinese patent number is CN200610022102.9's; Name is called a kind of patent of invention of method for preparing hydrogen by reforming methanol with high recovery rate; Comprise that methyl alcohol is mixed the back supercharging with water send into the vaporization superheater; Get into converter after reaching reaction temperature; Under catalyst action, reform and generate reformed gas; Again this reformed gas is cooled to normal temperature; Be set with in the pressure swing adsorption decarbonization device of decarburization adsorbent and slough carbon dioxide sending into one after this reformed gas purified treatment, obtain containing H
2, CO, CH
4The decarburization raw hydrogen; This decarburization raw hydrogen being sent into a cover is that the transformation absorption of main adsorbent is carried and sloughed all impurity in the hydrogen production device and promptly obtain product hydrogen with molecular sieve again; Incorporate into from the methyl alcohol of vaporization superheater and the mist entering converter of water after proposing the tail gas supercharging in the hydrogen production device; Tail gas in the decarbonization device directly discharges; Though this kind method can increase substantially the total yield of hydrogen; Reduce the hydrogen manufacturing cost; But owing to adopt two-phase method; Bigger to investment of devices; The plant area area is big, and the carbon monoxide rate of recovery is lower, is about 15%; The rate of recovery of High Purity Hydrogen is also lower, is about 91%.
Summary of the invention
The present invention solves mainly that two-phase method carries that hydrogen storage equipment investment is big, hydrogen recovery rate is lower, the technical problem that the rate of recovery is low, the hydrogen manufacturing cost is high of carbon monoxide and carbon dioxide; Provide a kind of and can fully reclaim method and the device that carbon monoxide and carbon dioxide, high, the total hydrogen rate of recovery of hydrogen purity is high, equipment investment is few, floor space is little, the device overall economic benefit is good one-stage process transformation absorption are carried hydrogen and reclaimed rich carbon gas.
In order to solve the technical problem of above-mentioned existence, the present invention adopts following technical proposals:
The absorption of one-stage process transformation is carried hydrogen and is reclaimed the method for rich carbon gas; Adopt the transformation absorption principle from methanol synthetic discharged gas delayed, to extract highly purified hydrogen as product gas; Reclaim the unstripped gas of the rich carbon gas of the high-purity that produces in the desorption process simultaneously as methanol device; And the higher concentration that produces be back to the methyl alcohol system along putting hydrogen; Low concentration enter the fuel pipe network along placing the ventilation gas that acts as a fuel; Each circulation in its technological process includes adsorption process; All process is pressed in pressure drop; Along letting slip journey; Replacement process; The contrary journey of letting slip; Vacuum; All voltage rise is pressed process and is broken through journey eventually, and concrete technological process is following:
A) adsorption process: the methanol synthetic discharged gas delayed absorption through import sequencing valve entering transformation after the unstripped gas cell processing carried in the adsorption tower that is in adsorbed state in the hydrogen unit; Under the selective absorption successively of multiple adsorbent, with the H in methanol synthetic discharged gas delayed
2O, alcohols, CO
2, CO, CH
4, N
2Absorb etc. component, components such as the hydrogen that is not adsorbed flow into the product tracheae from cat head through product gas sequencing valve, input in the hydrogen gas buffer in the product gas unit;
B) all process is pressed in pressure drop: after adsorption process finishes; Through all pressing sequencing valve; The hydrogen discharge of the elevated pressures in the adsorption tower is gone in other lower pressure adsorption tower of having accomplished regeneration along the absorption direction; This process is not only the step-down process; Reclaim the process of hydrogen in the adsorption bed dead space especially, this process can comprise that repeatedly depressurization step is to guarantee the abundant recovery of hydrogen;
C) along letting slip journey: after the drop pressure process finishes; With the hydrogen that also has certain pressure in the adsorption tower along broadcasting out; By getting into along putting the hydrogen air accumulator along the venting sequencing valve with along putting hydrogen control valve; Again be transmitted back to the methyl alcohol system, thereby this process can improve the lower pressure hydrogen recovery of adsorbent bed dead space total hydrogen rate of recovery of device;
D) replacement process: after letting slip the journey end; Rich carbon gas from elevated pressures in the displacement gas air accumulator gets into the adsorption tower bottom through the displacement sequencing valve; Nitrogen in the adsorbent bed and methane are swapped out along placing; The gas that cements out is through exporting the fuel pipe network to along venting sequencing valve and fuel gas control valve; This process can cement out nitrogen in the adsorption layer and methane; Improve the interior carbon dioxide of adsorption tower and the concentration of carbon monoxide; Also the carbon dioxide in the raising understanding gassing and the content of carbon monoxide reduce the content of separating nitrogen component in the gassing effectively;
E) the contrary journey of letting slip: after replacement process finishes, will also have the gas of certain pressure to drain into contrary venting surge tank through the displacement sequencing valve is contrary in the adsorption tower, and send into through pressure-regulating valve and to separate the gassing blending tank, the gas pressure in this moment adsorption tower is reduced to normal pressure;
F) vacuum: let slip after journey finishes contrary; Vavuum pump vacuumizes adsorption tower through vacuumizing sequencing valve; Pressure in the adsorption tower further reduces; The complete desorption of the component that is adsorbed is come out; Desorption gas is directly delivered to and is separated the gassing blending tank; A part of desorption gas of separating in the gassing blending tank is compressed the machine suction and compresses the back entering displacement gas air accumulator that boosts; Rich carbon gas as elevated pressures is that replacement process is got ready, and remaining desorption gas is then exported the unstripped gas that becomes methanol device again as rich carbon gas;
G) all process is pressed in voltage rise: after vacuum finishes, use from the elevated pressures hydrogen in other adsorption towers this adsorption tower is continued to boost, comprise the step of repeatedly boosting to guarantee the abundant recovery of hydrogen, this process presses process corresponding with equal pressure drop;
H) break through journey eventually: after the boost pressure process finishes; In order to make adsorption tower can steadily switch to next time adsorption process and to guarantee that the product Hydrogen Vapor Pressure does not fluctuate in this course; By slowly and reposefully sending into product gas in the adsorption tower towards sequencing valve eventually; Make the pressure in the adsorption tower rise to adsorptive pressure, guarantee product boost process fully with the influence that reduces the adsorptive pressure fluctuation;
I) several adsorption tower alternating sequences carry out above absorption-regenerative operation process, can realize the purpose to methanol synthetic discharged gas delayed continuous Separation & Purification.
The absorption of one-stage process transformation is carried hydrogen and is reclaimed the device of rich carbon gas; Comprise the unstripped gas unit; The hydrogen unit is carried in transformation absorption; Product gas unit; Conciliate the gassing unit along the venting unit; Methanol synthetic discharged gas delayedly after the unstripped gas cell processing, get into transformation absorption and carry the hydrogen unit; Extract high-purity hydrogen and export product gas unit to; The gas that desorption produces is after separating the gassing cell processing; Part desorption gas reenters transformation absorption as displacement gas and carries the hydrogen unit; Another part is recycled to the methyl alcohol system as rich carbon gas; To methanol synthetic discharged gas delayed; Hydrogen technology is put forward in transformation absorption through this device; Can extract highly purified hydrogen, the rich carbon gas that obtains high-load simultaneously is recycled to the methyl alcohol system.
As preferably; Said unstripped gas unit comprises inlet adjusting valve, superpressure control valve, metering valve and gas-liquid separator; Methanol synthetic discharged gas delayed through inlet adjusting valve reduction pressure; And the entering gas-liquid separator is handled behind the metering valve calculated flow rate; Unstripped gas after the processing gets into transformation absorption and carries the hydrogen unit; After unstripped gas process step-down and the gas-liquid separating treatment, reached transformation and adsorbed the requirement of putting forward hydrogen technology.
As preferably; Said transformation absorption is carried the hydrogen unit and is comprised some adsorption towers and corresponding sequencing valve; Transformation absorption is carried the hydrogen unit and is provided with the raw material gas inlet pipe; The adsorption tower outlet; The product tracheae; Balance pipe; Along bleeder pipe; Whole qi of chong channel ascending adversely pipe; The contrary pipe of putting of adsorption tower; Resolve tracheae and vacuum-pumping tube; Contrary the putting of the adsorption tower of said raw material gas inlet pipe and adsorption tower bottom is provided with the import sequencing valve between the pipe; Methanol synthetic discharged gas delayed through import sequencing valve entering adsorption tower; Be provided with product gas sequencing valve between the adsorption tower outlet at said product tracheae and adsorption tower top; The High Purity Hydrogen of transformation adsorbing and extracting flows into the product tracheae through product gas sequencing valve; And output to product gas unit; Be provided with between described balance pipe and the adsorption tower outlet and all press sequencing valve; The hydrogen that finishes the interior elevated pressures of adsorption tower of adsorption process can flow in the adsorption tower of the lower pressure that finishes regeneration through all pressing accordingly sequencing valve; Described along being provided with between bleeder pipe and the adsorption tower escape pipe along the venting sequencing valve; Suitable venting in the pressure-swing absorption process is through flowing into suitable bleeder pipe and exporting to along the venting unit along the venting sequencing valve; Be provided with between said whole qi of chong channel ascending adversely pipe and the adsorption tower outlet eventually towards sequencing valve; Can go into to accomplish in the adsorption tower through whole stroke control valve flow from the product gas of product gas unit and boost; Contrary the putting of said parsing tracheae and adsorption tower is provided with the displacement sequencing valve between the pipe; Desorption gas can flow into to resolve tracheae and be expelled to through the displacement sequencing valve separates the gassing unit; Simultaneously; Displacement gas also can flow into contrary the putting in pipe and the entering adsorption tower of adsorption tower through the displacement sequencing valve adsorbent is replaced; Said vacuum-pumping tube and adsorption tower vacuumize sequencing valve against putting to be provided with between the pipe; Remaining desorption gas in the adsorption tower is separated the gassing unit through vacuumizing sequencing valve entering vacuum-pumping tube and being expelled to; Through controlling each sequencing valve; Make the different adsorption tower be operated in the different stages; The absorption and the regenerative process that guarantee adsorption tower are continuous and steady; The hydrogen of dead space can be delivered in the other adsorption tower in the adsorbent bed; The gas of each component all obtains reclaiming and utilizing; Total hydrogen rate of recovery of device is high; Through utilizing of the displacement of rich carbon gas to adsorbent bed; Can improve and separate carbon monoxide and concentration of carbon dioxide in the gassing; Reduce and separate the nitrogen content in the gassing, reach and reclaim the purpose of separating gassing.
As preferably; The quantity of said adsorption tower is 6～12; The multitower cycle operation forms repeatedly all pressing in the absorption-regenerative process; Both reclaimed the high-purity hydrogen in the adsorbent bed dead space; Greatly improve the rate of recovery of hydrogen, reduced the pressure oscillation in the adsorbent bed again, prolonged the service life of adsorbent; The user can be according to actual needs and economic indicator, rationally selects the quantity of adsorption tower for use.
As preferably; Be provided with one or more adsorbents in the said adsorption tower; Said multiple adsorbent is pressed the absorption property compound adsorbent bed of layering filling composition successively; The different gas component of the corresponding absorption of different types of adsorbent; Can fully adsorb each gas component in methanol synthetic discharged gas delayed; Gas separation effect well and and then promoted device total hydrogen rate of recovery and rich carbon gas recovery rate, improved economic benefit.
As preferably; Said product gas unit comprises hydrogen gas buffer, Hydrogen Vapor Pressure control valve and whole qi of chong channel ascending adversely pressure-regulating valve; Said Hydrogen Vapor Pressure control valve one end is connected with the product tracheae; The other end is connected with hydrogen gas buffer; Said whole qi of chong channel ascending adversely pressure-regulating valve one end is connected with the product tracheae; The other end is connected with whole qi of chong channel ascending adversely pipe; The pressure that has guaranteed product hydrogen is steady; Satisfy the use needs; Simultaneously; Regulate whole qi of chong channel ascending adversely and make the pressure that finishes the regeneration adsorption tower can steadily rise to adsorptive pressure, reduce the influence of pressure oscillation adsorption process and adsorbent.
As preferably; Described suitable venting unit comprises along putting hydrogen control valve; Fuel gas control valve and the suitable hydrogen air accumulator of putting; Said along putting hydrogen control valve one end and being connected along bleeder pipe; The other end be connected along putting the hydrogen air accumulator; Said fuel gas control valve one end is connected with suitable bleeder pipe; The other end is connected with the fuel pipe network; The hydrogen of the elevated pressures in the adsorbent bed dead space is reclaimed again; Be recycled to the methyl alcohol system; Improved the total hydrogen rate of recovery of device, and cement out contain nitrogen; The low-pressure gas of methane can be used as fuel gas and delivers to the fuel pipe network; Make full use of, good in economic efficiency.
As preferably; The said gassing unit of separating comprises vavuum pump; Compressor; The displacement gas air accumulator; Contrary venting air accumulator is conciliate the gassing blending tank; The said gassing blending tank of separating is respectively equipped with two imports and two outlets; The outlet of said contrary venting air accumulator and separate between the import of gassing blending tank and be provided with pressure-regulating valve; One end of said pressure-regulating valve is connected with contrary venting air accumulator; The other end with separate the gassing blending tank and be connected; The import of contrary venting air accumulator is connected with the parsing tracheae through the desorption gas control valve; Another import of separating the gassing blending tank is connected with the vacuum delivery side of pump; The import of vavuum pump is connected with vacuum-pumping tube; Said compressor air suction mouth is connected with an outlet of separating the gassing blending tank; The exhaust outlet of compressor is connected with the displacement gas air accumulator; The other end of displacement gas air accumulator is connected with the parsing tracheae through the displacement gas control valve; After the desorption gas that is rich in carbon dioxide and carbon monoxide that the adsorption process desorption comes out is regulated through secondary; A part is compressed the machine compression and sends into the displacement gas air accumulator; As nitrogen in the displacement adsorbent bed; The displacement gas of gases such as methane; Can improve the carbon monoxide and the carbon dioxide content of desorption gas; Reduce the content of nitrogen in the desorption gas; Can in separating gassing, obtain highly purified rich carbon gas again; Be recycled to the methyl alcohol system; The favorable regeneration effect of vacuum desorption can improve the high purity of conciliating gassing of product yield.
As preferably, be provided with the displacement gas flow valve between said displacement gas air accumulator and the displacement gas control valve, can detect the flow of displacement gas in real time.
The invention has the beneficial effects as follows: compare with conventional two sections pressure swing adsorption methods:
1., adopt this kind method can reach reduced investment, cost performance is high;
2., install total hydrogen rate of recovery height, >=98%;
3., the product hydrogen recovery rate is high,>=94% (CO+CO2≤10PPM);
4., the carbon monoxide rate of recovery is high,>=80% (nitrogen content≤5%) helps the methyl alcohol raising the output;
5., technic index is reliable and stable, handling strong;
6., the device rationally distributed, floor space is little.
Description of drawings
Fig. 1 is a kind of process flow diagram of the present invention;
Fig. 2 is a kind of device sketch map of the present invention;
Fig. 3 is a kind of technological process time-scale of the present invention;
Fig. 4 is a kind of technological process operating parameter table of the present invention;
1. unstripped gas unit among the figure, 11. inlet adjusting valves, 12. superpressure control valves; 13. metering valve, 14. gas-liquid separators, 2. the hydrogen unit is carried in transformation absorption; 21. adsorption tower, 22. raw material gas inlet pipes, 23. adsorption tower outlets; 24. the product tracheae, 25. balance pipes, 26. along bleeder pipe; 27. whole qi of chong channel ascending adversely pipe, the contrary pipe of putting of 28. adsorption towers, 29. resolve tracheae; 30. vacuum-pumping tube, 31. import sequencing valves, 32. product gas sequencing valves; 33. all press sequencing valve, 34. along the venting sequencing valve, 35. eventually towards sequencing valve; 36. the displacement sequencing valve, 37. vacuumize sequencing valve, 4. product gas unit; 41. hydrogen gas buffer, 42. Hydrogen Vapor Pressure control valves, 43. whole qi of chong channel ascending adversely pressure-regulating valves; 5. along the venting unit, 51. along putting hydrogen control valve, 52. fuel gas control valves; 53., 6. separate the gassing unit, 61. vavuum pumps along putting the hydrogen air accumulator; 62. compressor, 63. displacement gas air accumulators, 64. contrary venting air accumulators; 65. separate the gassing blending tank, 66. pressure-regulating valves, 67. desorption gas control valves; 68. the displacement gas control valve, 69. displacement gas flow valves.
The specific embodiment
Pass through embodiment below, and combine accompanying drawing, do further bright specifically technical scheme of the present invention.
Embodiment: the one-stage process transformation absorption of present embodiment is carried hydrogen and is reclaimed the device of rich carbon gas; As shown in Figure 1; Adopt the transformation absorption principle from methanol synthetic discharged gas delayed, to extract highly purified hydrogen as product gas; Reclaim the unstripped gas of the rich carbon gas of the high-purity that produces in the desorption process simultaneously as methanol device; And the higher concentration that produces be back to the methyl alcohol system along putting hydrogen; Low concentration enter the fuel pipe network along placing the ventilation gas that acts as a fuel; Transformation absorption is carried the hydrogen unit and is adopted 10-2-6PR/VPSA; As shown in Figure 2; Adsorption tower quantity is 10; Wherein there are two adsorption towers to be in adsorbed state all the time; Pressure equalizing is 6 times; Each circulation in its technological process includes adsorption process; All process is pressed in pressure drop; Along letting slip journey; Replacement process; The contrary journey of letting slip; Vacuum; All voltage rise is pressed process and is broken through journey eventually; The technological process time-scale as shown in Figure 3; The operating parameter table of technological process as shown in Figure 4, concrete technological process (is example with the work of A tower) as follows:
A) adsorption process: the pressure that comes from the outside is 5.0Mpa; Temperature is 30 ℃ of these devices of methanol synthetic discharged gas delayed entering; After the unstripped gas cell processing; Be decompressed to 2.7 MPa; Get in the A tower through import sequencing valve 31A; Under the selective absorption successively of multiple adsorbent, with the H in methanol synthetic discharged gas delayed
2O, alcohols, CO
2, CO, CH
4, N
2Absorb etc. component, components such as the hydrogen that is not adsorbed flow into product tracheae 24 from cat head through product gas sequencing valve 32A, input in the hydrogen gas buffer in the product gas unit 4 41, and adsorption time is about 120 seconds;
B) all process is pressed in pressure drop: after adsorption process finishes; Close import sequencing valve 31A and product gas sequencing valve 32A; Open and all press sequencing valve 33A and 33D; Along adsorbing the D tower that direction is gone into the hydrogen discharge of 2.7 MPa in the A tower to accomplish regeneration; Time is 15 seconds, and A, D two pressure tower balances are 2.302 MPa at this moment;
Close and all press sequencing valve 33D, open and all press sequencing valve 33E, the hydrogen of 2.302 MPa flows into the E tower along the absorption direction in the A tower, and the time is 15 seconds, and A, E two pressure tower balances are 1.905 MPa at this moment;
Close and all press sequencing valve 33E, open and all press sequencing valve 33F, the hydrogen of 1.905 MPa flows into the F tower along the absorption direction in the A tower, and the time is 15 seconds, and A, F two pressure tower balances are 1.508MPa at this moment;
Close and all press sequencing valve 33F, open and all press sequencing valve 33G, the hydrogen of 1.508MPa flows into the G tower along the absorption direction in the A tower, and the time is 15 seconds, and A, G two pressure tower balances are 1.111 MPa at this moment;
Close and all press sequencing valve 33G, open and all press sequencing valve 33H, the hydrogen of 1.111 MPa flows into the H tower along the absorption direction in the A tower, and the time is 15 seconds, and A, H two pressure tower balances are 0.714 MPa at this moment;
Close and all press sequencing valve 33H, open and all press sequencing valve 33I, the hydrogen of 0.714 MPa flows into the I tower along the absorption direction in the A tower, and the time is 15 seconds, and A, I two pressure tower balances are 0.317 MPa at this moment;
C) along letting slip journey: after the drop pressure process finishes; Close and all press sequencing valve 33A and 33I, open along venting sequencing valve 34A with along putting hydrogen control valve 51, the hydrogen of 0.317 MPa flows into along putting hydrogen air accumulator 53 in the A tower; Time is 15 seconds, and the interior pressure of A tower this moment drops to 0.15 MPa;
D) replacement process: after letting slip the journey end; Close along putting hydrogen control valve 51; Open fuel gas control valve 52, displacement sequencing valve 36A and displacement gas control valve 68; Rich carbon gas from elevated pressures in the displacement gas air accumulator 63 gets into the A tower through displacement sequencing valve 36A; Nitrogen in the adsorbent bed and methane are swapped out along placing; The gas that cements out is through exporting the fuel pipe network to along venting sequencing valve 34A and fuel gas control valve; Time swap is 15 seconds, and the interior pressure of A tower this moment drops to 0.1 MPa;
E) the contrary journey of letting slip: after replacement process finishes; Close along venting sequencing valve 34A, fuel gas control valve 52 and displacement gas control valve 68; Open desorption gas control valve 67; The gas of 0.1 MPa is contrary in the A tower drains into against venting surge tank 64; And send into through pressure-regulating valve 66 and to separate gassing blending tank 65; The contrary time of putting is 15 seconds, and the interior pressure of A tower this moment is reduced to normal pressure;
F) vacuum: let slip after journey finishes contrary; Close desorption gas control valve 67 and displacement sequencing valve 36A; Open and vacuumize sequencing valve 37A and vavuum pump 61; The A tower is vacuumized; Pressure in the A tower further reduces; The complete desorption of the component that is adsorbed is come out; Desorption gas is directly delivered to and is separated gassing blending tank 65; A part of desorption gas of separating in the gassing blending tank is compressed machine 62 suctions and compresses the back entering displacement gas air accumulator 63 that boosts; Rich carbon gas as elevated pressures is that replacement process is got ready; Remaining desorption gas then as the output of rich carbon gas again as the unstripped gas of methanol device; Pumpdown time is 60 seconds, and the interior pressure of A tower this moment drops to-0.08MPa;
G) all process is pressed in voltage rise: after vacuum finishes; Close and vacuumize sequencing valve 37A and vavuum pump 61; Open and all press sequencing valve 33A and 33C; Along the absorption direction hydrogen of 0.714 MPa in the C tower is introduced the A tower of having accomplished regeneration; Time is 15 seconds, and A, C two pressure tower balances are 0.317 MPa at this moment;
Close and all press sequencing valve 33C, all press sequencing valve 33D through opening after the time-delay in 30 seconds, the hydrogen of 1.111MPa flows into the A tower along the absorption direction in the D tower, and the time is 15 seconds, and A, D two pressure tower balances are 0.714 MPa at this moment;
Close and all press sequencing valve 33D, all press sequencing valve 33E through opening after the time-delay in 30 seconds, the hydrogen of 1.508 MPa flows into the A tower along the absorption direction in the E tower, and the time is 15 seconds, and A, E two pressure tower balances are 1.111MPa at this moment;
Close and all press sequencing valve 33E, all press sequencing valve 33F through opening after the time-delay in 30 seconds, the hydrogen of 1.905MPa flows into the A tower along the absorption direction in the F tower, and the time is 15 seconds, and A, F two pressure tower balances are 1.508 MPa at this moment;
Close and all press sequencing valve 33F, all press sequencing valve 33G through opening after the time-delay in 30 seconds, the hydrogen of 2.302 MPa flows into the G tower along the absorption direction in the G tower, and the time is 15 seconds, and A, G two pressure tower balances are 1.905 MPa at this moment;
Close and all press sequencing valve 33G, all press sequencing valve 33H through opening after the time-delay in 30 seconds, the hydrogen of 2.7MPa flows into the A tower along the absorption direction in the H tower, and the time is 15 seconds, and A, H two pressure tower balances are 2.302 MPa at this moment;
Use from the elevated pressures hydrogen in other adsorption towers the A tower is continued to boost, comprise six steps of boosting to guarantee the abundant recovery of hydrogen, this process is with all pressure drop pressure process is corresponding;
H) break through journey eventually: after all voltage rise pressure process finishes, open eventually towards sequencing valve 35A, the product gas of 2.7 MPa flows in the A tower, and the time is 45 seconds, and the pressure in this moment A tower rises to 2.7 MPa, reaches the pressure requirement of absorption;
I) 10 adsorption tower alternating sequences carry out above absorption-regenerative operation process, can realize the purpose of the continuous Separation & Purification of unstripped gas.
More than explanation is not that the present invention has been done restriction; The present invention also is not limited only to giving an example of above-mentioned explanation; The variation that those skilled in the art have done in essential scope of the present invention, retrofit, increase or replace, all should be considered as protection scope of the present invention.
Claims (10)
1. an one-stage process transformation is adsorbed the method for carrying hydrogen and reclaiming rich carbon gas; Adopt the transformation absorption principle from methanol synthetic discharged gas delayed, to extract highly purified hydrogen; Reclaim the unstripped gas of the rich carbon gas of the high-purity that produces in the desorption process simultaneously as methanol device; And the higher concentration that produces be returned to the methyl alcohol system along putting hydrogen recovery; Low concentration enter the fuel pipe network along placing the ventilation gas that then acts as a fuel; Each circulation in its technological process includes adsorption process; All process is pressed in pressure drop; Along letting slip journey; Replacement process; The contrary journey of letting slip; Vacuum; All voltage rise is pressed process and is broken through journey eventually, and concrete technological process is following:
A) adsorption process: methanol synthetic discharged gas delayed after the unstripped gas cell processing gets into transformation absorption through the import sequencing valve and carries in the adsorption tower that is in adsorbed state in the hydrogen unit, under the selective absorption successively of multiple adsorbent, and the H in methanol synthetic discharged gas delayed
2O, alcohols, CO
2, CO, CH
4, N
2Be adsorbed etc. component, components such as the hydrogen that is not adsorbed flow into the product tracheae from cat head through product gas sequencing valve, input in the hydrogen gas buffer in the product gas unit;
B) all process is pressed in pressure drop: after adsorption process finishes; Through all pressing sequencing valve; Along the absorption direction with adsorption tower in the hydrogen discharge of elevated pressures go in other lower pressure adsorption tower of having accomplished regeneration; This process is not only the step-down process; Reclaim the process of hydrogen in the adsorption bed dead space especially, this process can comprise that repeatedly depressurization step is to guarantee the abundant recovery of hydrogen;
C) along letting slip journey: after the drop pressure process finishes; With the hydrogen that also has certain pressure in the adsorption tower along broadcasting out; By getting into along putting the hydrogen air accumulator along the venting sequencing valve with along putting hydrogen control valve; Again be transmitted back to the methyl alcohol system, thereby this process can improve the lower pressure hydrogen recovery of adsorbent bed dead space total hydrogen rate of recovery of device;
D) replacement process: after letting slip the journey end; Rich carbon gas from elevated pressures in the displacement gas air accumulator gets into the adsorption tower bottom through the displacement sequencing valve; Nitrogen in the adsorbent bed and methane are swapped out along placing; The gas that cements out is through exporting the fuel pipe network to along venting sequencing valve and fuel gas control valve; This process can cement out nitrogen in the adsorption layer and methane; Improve the interior carbon dioxide of adsorption tower and the concentration of carbon monoxide; Also the carbon dioxide in the raising understanding gassing and the content of carbon monoxide reduce the content of separating nitrogen component in the gassing effectively;
E) the contrary journey of letting slip: after replacement process finishes, will also have the gas of certain pressure to drain into contrary venting surge tank through the displacement sequencing valve is contrary in the adsorption tower, and send into through pressure-regulating valve and to separate the gassing blending tank, the gas pressure in this moment adsorption tower is reduced to normal pressure;
F) vacuum: let slip after journey finishes contrary; Vavuum pump vacuumizes adsorption tower through vacuumizing sequencing valve; Pressure in the adsorption tower further reduces; The complete desorption of the component that is adsorbed is come out; Desorption gas is directly delivered to and is separated the gassing blending tank; A part of desorption gas of separating in the gassing blending tank is compressed the machine suction and compresses the back entering displacement gas air accumulator that boosts; Rich carbon gas as elevated pressures is that replacement process is got ready, and remaining desorption gas is then exported the unstripped gas that becomes methanol device again as rich carbon gas;
G) all process is pressed in voltage rise: after vacuum finishes, use from the elevated pressures hydrogen in other adsorption towers this adsorption tower is continued to boost, comprise the step of repeatedly boosting to guarantee the abundant recovery of hydrogen, this process presses process corresponding with equal pressure drop;
H) break through journey eventually: after the boost pressure process finishes; In order to make adsorption tower can steadily switch to next time adsorption process and to guarantee that the product Hydrogen Vapor Pressure does not fluctuate in this course; By slowly and reposefully sending into product gas in the adsorption tower towards sequencing valve eventually; Make the pressure in the adsorption tower rise to adsorptive pressure, guarantee product boost process fully with the influence that reduces the adsorptive pressure fluctuation;
I) several adsorption tower alternating sequences carry out above absorption-regenerative operation process, can realize the purpose to methanol synthetic discharged gas delayed continuous Separation & Purification.
2. an one-stage process transformation is adsorbed the device of carrying hydrogen and reclaiming rich carbon gas; It is characterized in that: comprise unstripped gas unit (1); Hydrogen unit (2) is carried in transformation absorption; Product gas unit (4); Conciliate gassing unit (6) along venting unit (5); Methanol synthetic discharged gas delayedly after the unstripped gas cell processing, get into transformation absorption and carry the hydrogen unit; Extract high-purity hydrogen and export product gas unit to; The gas that desorption produces is after separating the gassing cell processing; Part desorption gas reenters transformation absorption as displacement gas and carries the hydrogen unit, and another part is recycled to the methyl alcohol system as rich carbon gas.
3. one-stage process transformation absorption according to claim 2 is carried hydrogen and is reclaimed the device of rich carbon gas; It is characterized in that: said unstripped gas unit (1) comprises inlet adjusting valve (11), superpressure control valve (12), metering valve (13) and gas-liquid separator (14); Methanol synthetic discharged gas delayed through inlet adjusting valve reduction pressure; And behind the metering valve calculated flow rate, getting into the gas-liquid separator processing, the unstripped gas after the processing gets into transformation absorption and carries the hydrogen unit.
4. one-stage process transformation absorption according to claim 2 is carried hydrogen and is reclaimed the device of rich carbon gas; It is characterized in that: said transformation absorption is carried hydrogen unit (2) and is comprised some adsorption tower (21A; B; C ...) and corresponding sequencing valve; Transformation absorption is carried the hydrogen unit and is provided with raw material gas inlet pipe (22); Adsorption tower outlet (23); Product tracheae (24); Balance pipe (25); Along bleeder pipe (26); Whole qi of chong channel ascending adversely pipe (27); The contrary pipe (28) of putting of adsorption tower; Resolve tracheae (29) and vacuum-pumping tube (30); Contrary the putting of the adsorption tower of said raw material gas inlet pipe and adsorption tower bottom is provided with import sequencing valve (31 A between the pipe; B; C ...); Methanol synthetic discharged gas delayed through import sequencing valve entering adsorption tower; Be provided with product gas sequencing valve (32 A between the adsorption tower outlet at said product tracheae and adsorption tower top; B; C ...); The High Purity Hydrogen of transformation adsorbing and extracting flows into the product tracheae through product gas sequencing valve; And output to product gas unit (4); Be provided with between described balance pipe and the adsorption tower outlet and all press sequencing valve (33A; B; C ...); The hydrogen that finishes the interior elevated pressures of adsorption tower of adsorption process can flow in the adsorption tower of the lower pressure that finishes regeneration through all pressing accordingly sequencing valve; Described along being provided with between bleeder pipe and the adsorption tower escape pipe along venting sequencing valve (34 A; B; C ...); Suitable venting in the pressure-swing absorption process is through flowing into suitable bleeder pipe and exporting to along venting unit (5) along the venting sequencing valve; Be provided with between said whole qi of chong channel ascending adversely pipe and the adsorption tower outlet eventually towards sequencing valve (35 A; B; C ...); Can go into to accomplish in the adsorption tower through whole stroke control valve flow from the product gas of product gas unit and boost; Contrary the putting of said parsing tracheae and adsorption tower is provided with displacement sequencing valve (36 A between the pipe; B; C ...); Desorption gas can flow into to resolve tracheae and be expelled to through the displacement sequencing valve separates gassing unit (6); Simultaneously; Displacement gas also can flow into contrary the putting in pipe and the entering adsorption tower of adsorption tower through the displacement sequencing valve adsorbent is replaced; Said vacuum-pumping tube and adsorption tower vacuumize sequencing valve (37 A against putting to be provided with between the pipe; B; C ...), the remaining desorption gas in the adsorption tower is separated the gassing unit through vacuumizing sequencing valve entering vacuum-pumping tube and being expelled to.
5. one-stage process transformation absorption according to claim 4 is carried hydrogen and is reclaimed the device of rich carbon gas, it is characterized in that: said adsorption tower (21 A, B, C ...) quantity be 6～12.
6. described according to claim 4 or 5, it is characterized in that: said adsorption tower (21 A, B, C ...) in be provided with one or more adsorbents, said multiple adsorbent press absorption property successively layering filling form compound adsorbent bed.
7. one-stage process transformation absorption according to claim 2 is carried hydrogen and is reclaimed the device of rich carbon gas; It is characterized in that: said product gas unit (4) comprises hydrogen gas buffer (41), Hydrogen Vapor Pressure control valve (42) and whole qi of chong channel ascending adversely pressure-regulating valve (43); Said Hydrogen Vapor Pressure control valve one end is connected with product tracheae (24); The other end is connected with hydrogen gas buffer; Said whole qi of chong channel ascending adversely pressure-regulating valve one end is connected with the product tracheae, and the other end is connected with whole qi of chong channel ascending adversely pipe (27).
8. one-stage process transformation absorption according to claim 2 is carried hydrogen and is reclaimed the device of rich carbon gas; It is characterized in that: said suitable venting unit (5) comprises along putting hydrogen control valve (51), fuel gas control valve (52) and the suitable hydrogen air accumulator (53) of putting; Said along putting hydrogen control valve one end and being connected along bleeder pipe (26); The other end be connected along putting the hydrogen air accumulator; Said fuel gas control valve one end is connected with suitable bleeder pipe, and the other end is connected with the fuel pipe network.
9. one-stage process transformation absorption according to claim 2 is carried hydrogen and is reclaimed the device of rich carbon gas; It is characterized in that: the said gassing unit (6) of separating comprises vavuum pump (61); Compressor (62); Displacement gas air accumulator (63); Contrary venting air accumulator (64) is conciliate gassing blending tank (65); The said gassing blending tank of separating is respectively equipped with two imports and two outlets; The outlet of said contrary venting air accumulator and separate between the import of gassing blending tank and be provided with pressure-regulating valve (66); One end of said pressure-regulating valve is connected with contrary venting air accumulator; The other end with separate the gassing blending tank and be connected; The import of contrary venting air accumulator is connected with parsing tracheae (29) through desorption gas control valve (67); Another import of separating the gassing blending tank is connected with the vacuum delivery side of pump; The import of vavuum pump is connected with vacuum-pumping tube (30); Said compressor air suction mouth is connected with an outlet of separating the gassing blending tank; The exhaust outlet of compressor is connected with the displacement gas air accumulator, and the other end of displacement gas air accumulator is connected with the parsing tracheae through displacement gas control valve (68).
10. one-stage process transformation absorption according to claim 9 is carried hydrogen and is reclaimed the device of rich carbon gas, it is characterized in that: be provided with displacement gas flow valve (69) between said displacement gas air accumulator (63) and the displacement gas control valve (68).
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1349841A (en) * | 2000-10-19 | 2002-05-22 | 四川华泰投资有限责任公司 | Pressure swing absorption process of separating relieved gas from methanol synthesis to prepare high-purity hydrogen and CO2 |
| CN1944239A (en) * | 2006-10-24 | 2007-04-11 | 四川亚连科技有限责任公司 | Method for preparing hydrogen by reforming methanol with high recovery rate |
-
2011
- 2011-07-08 CN CN201110190697.XA patent/CN102343196B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1349841A (en) * | 2000-10-19 | 2002-05-22 | 四川华泰投资有限责任公司 | Pressure swing absorption process of separating relieved gas from methanol synthesis to prepare high-purity hydrogen and CO2 |
| CN1944239A (en) * | 2006-10-24 | 2007-04-11 | 四川亚连科技有限责任公司 | Method for preparing hydrogen by reforming methanol with high recovery rate |
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Denomination of invention: Method and device for one-stage pressure swing adsorption hydrogen extraction and carbon-rich gas recovery Effective date of registration: 20170505 Granted publication date: 20140507 Pledgee: Zhejiang Fuyang Rural Commercial Bank branch of the new Limited by Share Ltd Pledgor: Hangzhou Perfect Purity Installation Co., Ltd. Registration number: 2017990000377 |