CN101104127A - Method and device for absorptive drying - Google Patents
Method and device for absorptive drying Download PDFInfo
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- CN101104127A CN101104127A CNA2006100287990A CN200610028799A CN101104127A CN 101104127 A CN101104127 A CN 101104127A CN A2006100287990 A CNA2006100287990 A CN A2006100287990A CN 200610028799 A CN200610028799 A CN 200610028799A CN 101104127 A CN101104127 A CN 101104127A
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Abstract
The invention provides an adsorption and drying method, which includes a adsorption phase and a regeneration phase. In the regeneration phase, part of the feed gas after the adsorption and drying is taken as the regeneration gas for implementing the reverse heating regeneration and cold blast, after being separated for free water by receiving the cooling again, the regeneration gas directly goes back to the middle part of a drying system instead of passing through the supercharger, and then the product gas can be obtained after the adsorption and drying. The invention also provides a device for drying by using the method. The adsorption and drying method of the invention is safe, energy-saving and is convenient to maintain.
Description
Technical field
The present invention relates to a kind of drying means, relate to adsorption and drying method particularly.
Background technology
Current, gas drying process is divided into two big classes: adsorption dry and freeze drying.
The adsorption dry of gas belongs to solid and gas two-phase mass transport process, its process is made up of the absorption and two stages of regenerating, and wherein the regeneration of adsorbent is a very important aspect that realizes the gas drying, its process of regenerating and effect directly influence the dew point of the body of regulating the flow of vital energy of living in, the specific energy consumption and the air feed continuation of device operation.
If the aridity of product gas being required when very high, be-60～-90 ℃ as dew point, the quality requirement that adopts general adsorption and drying method to be difficult to reach required maybe can arrive but energy consumption is high excessively.
When gas to be dried is inflammable toxic gases such as hydrogen, carbon monoxide, methane, natural gas and when being afraid of contaminated various high-purity gas, generally need carry out the closed cycle Gas reclamation.In closed cycle Gas reclamation process, as mentioned above in order to keep operating pressure, just need to adopt supercharger can make adsorption drying process continue to carry out.And adopt the weak point of supercharger to be: power consumption, troublesome maintenance, simultaneously because moving device long-term operation easily produces fault, leak easily and influence the quality of gas and produce shortcoming such as potential safety hazard.
In sum, this area lacks adsorption and drying method and device thereof safe, energy-conservation, easy maintenance.Therefore, this area presses for that exploitation is a kind of to be need not supercharger and realize that dry regeneration gas carries out reverse regeneration, and does not have the drying means and the device of regeneration gas emptying.
Summary of the invention
The objective of the invention is to obtain a kind ofly need not supercharger and realize that dry regeneration gas carries out reverse regeneration, and do not have the drying means of regeneration gas emptying.
Another object of the present invention is to obtain a kind ofly need not supercharger and realize that dry regeneration gas carries out reverse regeneration, and do not have the drying device of regeneration gas emptying.
One aspect of the present invention provides a kind of adsorption and drying method, comprises drying steps (A) and regeneration step (B), adopts first drying unit and second drying unit of series connection in the described drying steps (A), and the pressure of described second drying unit is less than first drying unit;
Adopt first regeneration unit and second regeneration unit of series connection in the described regeneration step (B), the pressure of described second regeneration unit is greater than first regeneration unit;
And said method comprising the steps of:
(A) drying steps:
(A-1) after water-containing material gas carries out adsorption dry in first drying unit, obtain adsorption dry gas;
(A-2) portion gas of the adsorption dry gas of step (A-1) enters second regeneration unit as regeneration gas, and the surplus portion gas is collected after the second drying unit drying and obtained product gas;
(B) regeneration step:
(B-1) the regeneration gas reverse flow that obtains of step (A-2) enters second regeneration unit and first regeneration unit is regenerated in regular turn, isolate free water after, the regeneration gas that is tentatively dewatered;
(B-2) air inlet that comes back to second drying unit and second drying unit of the regeneration gas that dewaters in the step (B-1) merges the back drying and obtains product gas.
In preferred implementation of the present invention, the described regeneration gas in the step (A-2) accounts for the 5-50 volume % of described adsorption dry gas.
In preferred implementation of the present invention, the dew point of the regeneration gas that tentatively dewaters in the step (B-1) is 10～40 ℃.
In preferred implementation of the present invention, the pressure of second drying unit is 5～200Kpa less than the pressure differential of first drying unit.
In preferred implementation of the present invention, the pressure of second regeneration unit is 1～50Kpa greater than the pressure differential of first regeneration unit.
In preferred implementation of the present invention, (A-1) dew point of the adsorption dry gas that obtains of step is-40 ℃～-90 ℃.
In preferred implementation of the present invention, the water content of water-containing material gas includes but not limited to saturation moisture content in the step (A-1).Obviously, the unstripped gas that is lower than saturation moisture content also is applicable to adsorption and drying method of the present invention.
In preferred implementation of the present invention, regeneration gas adds ripe 30-600 ℃ in the step (B-1) when reverse flow.
In preference of the present invention, preferred 60～400 ℃ of the temperature that regeneration gas heats when reverse flow; Further, can carry out blast-cold to room temperature with regeneration gas, for example 15-35 ℃ to the drier after the heating simultaneously.
In preferred implementation of the present invention, the moisture content of separating sucking-off in the described step (B-1) in the regeneration gas adopts the cooling method cooling, and then isolates free water.
In preferred implementation of the present invention, drying steps (A) and regeneration step (B) can be switched mutually, and promptly first drying unit and the second dry nonoculture are regeneration unit, and first regeneration unit and second regeneration unit are as drying unit.
In preferred implementation of the present invention,
Step (A-2) or (B-2) in the dew point of described product gas be-40 ℃～-90 ℃, and/or
The operating pressure of the described unstrpped gas in the step (A-1) is 0.03～16Mpa.
In preferred implementation of the present invention, described unstrpped gas is inflammable, explosive, poisonous gas and high-purity gas.
In a preferred embodiment of the invention, described flammable explosive gas is selected from hydrogen, carbon monoxide, methane, natural gas or its combination, described toxic gas is selected from ammonia, hydrogen sulfide, carbon monoxide, hydrogen chloride, sulfur dioxide, methyl alcohol or its combination, the purity of described high-purity gas is greater than 99.9%, and for example 99.9%～99.9999%.
In the preferred embodiments of the present invention, described unstrpped gas is: hydrogen, carbon monoxide, methane, natural gas or its combination.
The present invention provides a kind of adsorption dry device on the other hand, comprises drying unit and regeneration unit in parallel,
Comprise first drying unit and second drying unit of series connection in the described drying unit, between described first drying unit and second drying unit regulator be set,
Described regeneration unit comprises first regeneration unit and second regeneration unit of series connection, between described first regeneration unit and second regeneration unit regulator is set;
Be provided with path between described drying unit and the regeneration unit, comprise:
Enter the path of second regeneration unit for regeneration gas from first drying unit,
With the path that enters second drying unit for regeneration gas from first regeneration unit.
In preference of the present invention, the pressure drop loss is 10-500kPa.
In preferred implementation of the present invention, described regulator is one or more pressure regulation pressure-reducing valves.
In preferred implementation of the present invention, described pressure regulation pressure-reducing valve one or more check valves also in parallel.
In preference of the present invention, regulator of the present invention comprises two decompression valves and two check valves, in order to the realization of performing step closed cycle and the distribution of regeneration tolerance.
Description of drawings
Fig. 1 is adsorption and drying method flow process of the present invention and device schematic diagram thereof.
The specific embodiment
The inventor is through extensive and deep research, by improving one's methods and installing, obtained not need to adopt the gas absorption drying means of supercharger, and be surprised to find that the effect that the method is used for closed cycle gas is carried out adsorption dry is excellent especially, so be particularly suitable as inflammable toxic gas such as hydrogen, carbon monoxide, methane, natural gas and be afraid of the drying means of contaminated various high-purity gas.Finished the present invention on this basis.
As do not have on the contrary and indicate, the absorber among the present invention is adsorption dehumifier.
Regeneration gas
Regeneration gas of the present invention also claims purgative gas, and its effect is the moisture desorb that drier is adsorbed and takes in dry unit (concrete example such as drying tower) out of.The regeneration of drier is the combination of heat transfer and mass transport process.Regenerate when the lower regeneration gas of the higher aridity of temperature enters drier, the adsorbent in the heat drier makes it carry out desorb on the one hand; On the other hand, institute's water content is diffused in the regeneration gas and is pulled away in the adsorbent, and therefore, the aridity of regeneration gas directly has influence on the disposal ability of the regeneration effect and the drier of adsorbent.Simultaneously, the difference of regeneration has determined the difference of selected regeneration gas reflux ratio.The present invention adopt a part (as 5～50%) through the gas of preliminarily dried as regeneration gas, carry out reverse regeneration.Its advantage is that dry regeneration gas is carried out reverse regeneration and can be reached darker aridity, and this regeneration to adsorbent simultaneously is favourable, can guarantee that product gas reaches the dry preferably degree of depth, and dew point can reach-40 ℃～-90 ℃ D.P.
It is opposite that flow direction when " the reverse regeneration " of indication of the present invention is defined as gas and is in drying stage and regeneration gas are in the flow direction of regeneration during the stage.
In the present invention, unstrpped gas is carried out adsorption dry in first drying unit after, obtain dew point and be-40 ℃～-90 ℃ adsorption dry gas; The gas of 5-50 volume % wherein, preferred 5-40% enters the regeneration stage as regeneration gas.Regeneration gas of the present invention is dry gas (" dry gas " of the present invention refers to the gas that water content is lower, and promptly dew point is-40 ℃～-90 ℃ an adsorption dry gas).The regeneration gas reverse flow enters second regeneration unit and first regeneration unit is regenerated, and regeneration gas is isolated (preferably adopting cooling method to separate) behind the free water, obtains the regeneration gas under the normal temperature dew point; The air inlet merging back drying that the regeneration gas that dewaters comes back to second drying unit and second drying unit obtains product gas.
In preference of the present invention, regeneration gas heats 30-600 ℃ in reverse flow, preferred 60～400 ℃; Simultaneously, the drier after the heating is carried out blast-cold to room temperature with regeneration gas, for example 15-35 ℃.
Usually to carry out emptying or carry out supercharging the drying of general gas in the prior art.But the gas of Chu Liing is inflammable and explosive, poisonous, high-purity or expensive gas if desired, for example hydrogen, carbon monoxide, methane, natural gas etc., then whole system need carry out airtight can't emptying.Just must increase a supercharging device system is carried out supercharging this moment in system.Obviously, increased a supercharger and not only made system complicated more, and caused potential safety hazard.
And regeneration gas of the present invention is a dry gas, reverse regeneration, not emptying of regeneration gas.It is that closed cycle is not emptying of regeneration gas that system does not have the supercharger regeneration cycle, is specially adapted to inflammable poisonous and high-purity, expensive gas; Do not adopt supercharger, maintenance easy to use.
Adsorption desiccant
Absorption is because of adsorbate and sorbent molecule interphase interaction adsorption molecule a kind of effect of border transfer mutually to take place.Adsorption desiccant of the present invention is meant by suction-operated gas is carried out dry material.
In drying unit of the present invention and the regeneration unit, can adopt molecular sieve, activated alumina, silica gel or its combination to carry out drying as adsorbent.Can adopt identical drier between each drying unit, also can adopt different drier, for example: first, second drying unit can adopt identical drier, also can adopt different drier.Simultaneously, drying unit and regeneration unit are symmetric relations, and promptly first drying unit should load identical drier with first regeneration unit, second drying unit and second regeneration unit.
When gas to be dried fully contacted with adsorbent, the water diffusion in the gas was adsorbed to adsorbent and because of Van der Waals force.Meanwhile, the hydrone that is adsorbed is because of itself warm-up movement and the collision of extraneous gaseous molecular, and some leaves adsorbent surface and returns gas phase, and desorption promptly takes place.When the adsorbance of hydrone in the same time equates with desorption rate, just reached a dynamic adsorption equilibrium, this moment, absorption was all carried out with desorption process, but speed equates that this dynamic adsorption equilibrium is set up under uniform temperature and pressure condition.When temperature and pressure changes, the original equilibrium relation of system will be broken and be set up a new equilibrium relation.
Drying unit and regeneration unit
Adsorption dry device of the present invention comprises drying unit and regeneration unit, first drying unit and second drying unit that comprise series connection in the drying unit, the pressure of described second drying unit is less than first drying unit, regeneration unit comprises first regeneration unit and second regeneration unit of series connection, and the pressure of described second regeneration unit is greater than first regeneration unit.
First drying unit can be arranged on the top of second drying unit, also can be arranged on the below of second drying unit.
First regeneration unit can be arranged on the top of second regeneration unit, also can be arranged on the below of second regeneration unit.
Between first drying unit of the present invention and second drying unit regulator is set, the direction of described regulator is: reduce pressure to second drying unit from first drying unit; Between first regeneration unit and second regeneration unit regulator is set, the direction of described regulator is: reduce pressure to first regeneration unit from second regeneration unit, make second to regenerate unimpededly to the first regeneration unit passage, pressure drop is simultaneously fallen.
Be provided with between the drying unit of described series connection and the regeneration unit for regeneration gas and enter the path of second regeneration unit and supply regeneration gas to enter the path of second drying unit from first regeneration unit from first drying unit.
Can comprise other more secondary units on the drying unit, for example the 3rd drying unit, the 4th drying unit connect according to the method for attachment of prior art, as serial or parallel connection to first and second drying units.
Can comprise other more secondary units in the regeneration unit, for example the 3rd regeneration unit, the 4th regeneration unit connect according to the method for attachment of prior art, as serial or parallel connection to first and second regeneration units.
When handing over dress, first drying unit can be installed in according to circumstances second drying unit above or below or side, first regeneration unit can be installed in according to circumstances second regeneration unit above or below or side.
In one embodiment of the invention, the adsorption dry device is made up of drying unit and regeneration unit, promptly usually said double-tower type.Wherein drying unit is made up of the first drying unit drier and the second drying unit drier of series connection.Regeneration unit is made up of the first regeneration unit drier and the second regeneration unit drier of series connection.Regulator is decompression valve and check valve.Drying unit adsorbs, and regeneration unit carries out desorb.The gas alternating current is through two tower type containers (being drying unit and regeneration unit) that are full of adsorbent, when one tower (being drying unit) adsorbs under operating pressure (high aqueous vapor dividing potential drop) state, then (TSA method) desorb under heating status of another tower (being regeneration unit) is switched two tower alternations by the program that sets then.
During use, take out regeneration gas in the utilization, control by decompression valve and check valve, make through the regeneration gas of epimere absorber drying and can before decompression valve, extract out, another group absorber of reverse regeneration, again behind cooler and separator, get back to decompression valve again after, discharge as product gas after continuing to enter hypomere drier drying.Refrigerated separation after the regeneration makes the water in system's dry run, can discharge as free water in separator, and then regeneration gas is got back in the absorber again, thereby has realized that regeneration gas does not need the purpose of emptying.
Drying unit of the present invention and regeneration unit can switch.Can realize manually by the keying of 12 two-port valves in parallel (or corresponding threeway, cross valve) or automatically switch such as, but be not limited to, two groups switching.During automatic switchover, for example, the job order of device and working time are controlled automatically by controller and finish.
Absorbed type drying device of the present invention can according to those skilled in the art know the following correlated condition of technical basis and selectivity parameter calculates, finally determine adsorbent loadings and structure.For example design according to following condition:
Field condition--environment temperature, system configuration
Inlet conditions--pressure, temperature, flow
Outlet operating mode--dew point, the pressure loss, effectively air demand
Service condition--dew point control mode, the equilibrium of supply and demand
Select parameter--adsorbent kind, dynamic adsorbance, the work period, safety (affluence) coefficient, the void tower flow velocity,
Time of contact, regeneration gas reflux ratio, heater power, time-program(me) etc.
For example, admission pressure 0.4MPa, 25 ℃ of intake air temperature, dew point-10 ℃ (or and the reflux ratio determined according to different regenerations design.Stipulating that when drier the worker avales when operation, its efficient will farthest be brought into play.As long as the technical staff is according to processing tolerance and the demand of common practise according to self, select the parameter that adapts, just can obtain the dry gas of required quality requirements.
Before the drier air inlet, oil removal filter can be set, enter the gas oil content of drier with reduction.
In one embodiment of the invention, because the absorber in drying unit and the regeneration unit is carried out segmentation, for example be divided into two sections, in take out regeneration gas, decompression valve is set and check valve is realized closed cycle.Regeneration tolerance adjustable joint is specially adapted to the adsorption dry of inflammable poisonous, high-purity gas, can reach energy-saving and cost-reducing, safety, convenient and reliable, and drying effect is good.
Simultaneously, rational venting channels has guaranteed the pressure and the dew point of stable and consistent; Guarantee air-flow evenly by desiccant layer, the elimination channeling; And make the time of contact of gas and drier longer, satisfy the dew point requirement of finished product gas.
Regulator
Between first drying unit of invention and second drying unit regulator is set, between first regeneration unit and second regeneration unit regulator is set.
In an embodiment of the present invention, regulator is one or more pressure regulation pressure-reducing valves, and its effect is a pressure of regulating and reduce drying.
Preferably, described pressure regulation pressure-reducing valve one or more check valves also in parallel, its effect is that regeneration gas is passed through under the pressure drop condition of dawn as far as possible smoothly.
Heater
The present invention is provided with heater.Heater can be electrical heating type or steam formula heater etc.Heater is arranged on regeneration gas to carry out on the passage of reverse flow.For example, heater is installed in regeneration unit upstream or side etc.
Coupling
Adsorption and drying method of the present invention can be used in combination with other method.
Adsorption dry device of the present invention also can carry out coupling with other device, to reach better drying effect.For example, at pending air water capacity height, and to handling the strict occasion of water capacity of back air, the normal drying system that adopts freeze drying and adsorption dry combination, the former is that the latter's prime is handled, corresponding like this load and the capacity that alleviates adsorption dry, and guarantee the needed dry degree of depth, have effect preferably.
(1) to the system of air pressure dew point requirement, adopt freeze drying process usually more than or equal to 2 ℃, otherwise, adsorption dry technology then adopted;
(2) big to the air-treatment amount, and the high system of water capacity, in conjunction with customer requirements, carry out energy consumption, Technological Economy such as expense of device and determine it is to adopt freeze drying process after relatively, still adopt adsorption dry technology or freezing, adsorption dry group technology.
The present invention has following characteristics compared with the prior art:
One. no regeneration gas emptying, good economy performance.
Two. no potential safety hazard, the discharging of no flammable explosive gas.
Three. environmental protection, there is not poisonous and hazardous gas discharging.
Four. no supercharger, saved the problems such as maintenance that supercharger brought, energy-saving and cost-reducing.
Five. product drying degree height.
Six. the automaticity height, it is fast convenient to open.
Seven. the adsorption dry that is specially adapted to inflammable toxic gas such as hydrogen, carbon monoxide, methane, natural gas and various high-purity gas is handled.
Below in conjunction with specific embodiment, further illustrate the present invention.Should be understood that these embodiment only to be used to the present invention is described and be not used in and limit the scope of the invention.The experimental technique of unreceipted actual conditions in the following example, usually according to normal condition, or the condition of advising according to manufacturer.Ratio and percentage are based on weight, unless stated otherwise.
Embodiment 1
Unstripped gas Q1 of the present invention is: the High Purity Hydrogen that water electrolysis hydrogen producing is made behind deoxygenation, water, the air inflow of described unstripped gas Q1-are 10～500Nm
3/ h, temperature is 35 ℃, pressure is 0.8MPa.
As shown in Figure 1,10～500Nm
3The dew point of/h is the import 1a that the unstripped gas Q1 under 35 ℃ enters first drying unit 1, carries out adsorption dry in first drying unit 1.Obtain dew point at the outlet 1b of first drying unit and be-70 ℃ adsorption dry gas Q2.
The 30 volume % part of adsorption dry gas Q2 is as regeneration gas Q21.Regeneration gas also can be 5-50 volume ratio %.The gas Q22 of surplus 70 volume % enters the inlet 2a of second drying unit 2 through pressure regulator valve F1.Simultaneously and pressure regulator valve F1 parallel connection be check valve F3.Before entering pressure regulator valve, the pressure 0.75MPa of Q22.Through the pressure regulator valve decompression, the pressure of Q22 is 0.6MPa.
Regeneration gas Q21 enters the import 4a of second regeneration unit 4 by path L1.Path L1 enters second regeneration unit 4 for regeneration gas Q21 from first drying unit 1.Promptly, regeneration gas Q21 does not enter pressure regulation pressure-reducing valve F1, but extracts out before entering F1 yet.The pressure that the initial pressure of regeneration gas Q21 is first drying unit outlet 1b is 0.75MPa.Regeneration gas Q21 passes through reverse inflow second regeneration unit 4 of valve F14 after entering heater 5 (5a suitable for reading of heater 5 is communicated with valve F9, and end opening 5b is communicated with the import 4a of second regeneration unit 4) by valve F9 again.Reverse implication is: the gas flow direction was opposite when the flow direction of regeneration gas Q21 and regeneration unit 3,4 used as drier.The pressure of the import 4a of second regeneration unit 4 is 0.72MPa.
Q21 enters first regeneration unit 3 and arrives second drying unit by path L2 then after second regeneration unit 4 is regenerated.Path L2 enters second drying unit 2 for regeneration gas Q21 from first regeneration unit 3.Also promptly, after the outlet 4b discharge of gas Q21 by second regeneration unit 4, this moment, valve F2 and valve F10 closed, and gas Q21 enters the import 3a of first regeneration unit 3 by check valve F4.After gas Q21 regenerates, enter cooler 6 by the valve F8 (this moment, valve F7 closed) that opens in first regeneration unit 3.The downstream of cooler 6 is provided with separator 7.Gas Q21 enters the import 2a of second drier 2 by the valve F11 that opens.At this moment, gas Q3 and Q22 merge and enter second drier 2.
The switching that I, II are two groups can realize manually by the keying of 12 in parallel two-port valve F5-F16 (or corresponding threeway, cross valve) or automatically switch.Valve switches, the regeneration heating, and the free water discharging all can manually or automatically be carried out.
After second drying unit, 2 dryings, collect and obtain product gas Q4;
The dried dew point of product gas Q4 is-80 ℃ of D.P..
All quote in this application as a reference at all documents that the present invention mentions, just quoted as a reference separately as each piece document.Should be understood that in addition those skilled in the art can make various changes or modifications the present invention after having read above-mentioned instruction content of the present invention, these equivalent form of values fall within the application's appended claims institute restricted portion equally.
Claims (9)
1. an adsorption and drying method comprises drying steps (A) and regeneration step (B), it is characterized in that,
Adopt first drying unit (1) and second drying unit (2) of series connection in the described drying steps (A), the pressure of described second drying unit (2) is less than first drying unit (1);
Adopt first regeneration unit (3) and second regeneration unit (4) of series connection in the described regeneration step (B), the pressure of described second regeneration unit (4) is greater than first regeneration unit (3);
And said method comprising the steps of:
(A) drying steps:
(A-1) after water-containing material gas (Q1) carries out adsorption dry in first drying unit (1), obtain adsorption dry gas (Q2);
(A-2) portion gas of the adsorption dry gas (Q2) of step (A-1) enters second regeneration unit (4) as regeneration gas (Q21), and surplus portion gas (Q22) is collected after second drying unit (2) drying and obtained product gas (Q4);
(B) regeneration step:
(B-1) regeneration gas (Q21) reverse flow that obtains of step (A-2) enters second regeneration unit (4) and first regeneration unit (3) is regenerated in regular turn, isolate free water after, the regeneration gas that is tentatively dewatered (Q3);
(B-2) air inlet (Q22) that comes back to second drying unit (2) and second drying unit (2) of the regeneration gas that dewaters (Q3) in the step (B-1) merges the back drying and obtains product gas (Q4).
2. drying means according to claim 1 is characterized in that, regeneration gas (Q21) heats 30-600 ℃ in the step (B-1) when reverse flow.
3. drying means according to claim 1 is characterized in that, the moisture content of separating sucking-off in the described step (B-1) in the regeneration gas (Q21) adopts the cooling method cooling, and then isolates free water.
4. drying means according to claim 1, it is characterized in that, drying steps (A) and regeneration step (B) can be switched mutually, and promptly first drying unit (1) and second drying unit (2) be as regeneration unit, and first regeneration unit (3) and second regeneration unit (4) are as drying unit.
5. drying means according to claim 1 is characterized in that,
Step (A-2) or (B-2) in the dew point of described product gas (Q4) be-40 ℃～-90 ℃, and/or
The operating pressure of the described unstrpped gas (Q1) in the step (A-1) is 0.03～16Mpa.
6. drying means according to claim 1 is characterized in that, described unstrpped gas is inflammable, explosive, poisonous gas or high-purity gas.
7. an adsorption dry device comprises drying unit and regeneration unit in parallel, it is characterized in that,
Comprise first drying unit (1) and second drying unit (2) of series connection in the described drying unit, between described first drying unit (1) and second drying unit (2) regulator be set,
Described regeneration unit comprises first regeneration unit (3) and second regeneration unit (4) of series connection, between described first regeneration unit (3) and second regeneration unit (4) regulator is set;
Be provided with path between described drying unit and the regeneration unit, comprise:
Enter the path (L1) of second regeneration unit (4) for regeneration gas (Q21) from first drying unit (1),
With the path (L2) that enters second drying unit (2) for regeneration gas (Q21) from first regeneration unit (3).
8. device according to claim 7 is characterized in that, described regulator is one or more pressure regulation pressure-reducing valves.
9. device according to claim 7 is characterized in that, described pressure regulation pressure-reducing valve one or more check valves also in parallel.
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| CN102958583A (en) * | 2010-08-18 | 2013-03-06 | 环球油品公司 | Process for purifying natural gas and regenerating one or more adsorbers |
| CN102205200A (en) * | 2011-05-18 | 2011-10-05 | 中国计量科学研究院 | Gas drying system and method |
| CN102580457B (en) * | 2012-03-23 | 2014-07-16 | 苏州苏净保护气氛有限公司 | Oxygen generating device special for ozone device |
| CN102580457A (en) * | 2012-03-23 | 2012-07-18 | 苏州苏净保护气氛有限公司 | Oxygen generating device special for ozone device |
| CN103157353A (en) * | 2013-04-12 | 2013-06-19 | 北京安珂罗工程技术有限公司 | System and method for adsorbing and drying gas |
| CN103254955A (en) * | 2013-05-02 | 2013-08-21 | 中国海洋石油总公司 | Closed-type three-tower molecular sieve dehydration device |
| CN103254955B (en) * | 2013-05-02 | 2014-12-24 | 中国海洋石油总公司 | Closed-type three-tower molecular sieve dehydration device |
| CN104332083A (en) * | 2014-10-31 | 2015-02-04 | 徐州工程学院 | Adsorbent adsorption-regeneration presentation device and presentation method thereof |
| CN107847851A (en) * | 2015-09-02 | 2018-03-27 | 埃克森美孚上游研究公司 | The change adsorption method and system for cleaning gas are used as using demethanizer overhead stream |
| CN107847851B (en) * | 2015-09-02 | 2021-05-18 | 埃克森美孚上游研究公司 | Swing adsorption process and system using demethanizer overhead stream as purge gas |
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