CN102205235A - Method and apparatus for circulating, desorbing, shunting, recovering, and reclaiming hot gas by using adsorption bed - Google Patents
Method and apparatus for circulating, desorbing, shunting, recovering, and reclaiming hot gas by using adsorption bed Download PDFInfo
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Abstract
The invention belongs to the field of chemical separation and environment protection, and specifically relates to a method for circulating, desorbing, shunting, recovering, and reclaiming hot gas by using an adsorption bed. According to the present invention, a combined technology is adopted, that hot gas is circulated and desorbed by an adsorption bed, part of the desorbed gas is processed through bypass heat exchange, and the desorbed gas is condensed and recovered. With the method and the apparatus provided by the present invention, hot gas reclaiming procedures are carried out economically and effectively with the absorption bed. In prior arts, the energy consumption during hot gas desorbing is high, and the cost of hot exchange equipment is high. With the techniques of the present invention, the limitations are solved, and an advantage of hot gas desorbing technology is maintained, that organic matters recovered with a hot gas desorbing technology have relatively pure quality. The method and the apparatus provided by the present invention can be applied in the occasions of chemical adsorption separation, polluted gas purification, and organic solvents recovery. The method and the apparatus are especially suitable for the recovery of continuously discharged organic tail gas with a large total discharge amount. The recovery rate is higher than 90%.
Description
Technical field
The invention belongs to chemical separating, environmental technology field, be specifically related to a kind of adsorbent bed circulating desorption distributary recovery regeneration process and device thereof.
Background technology
Absorption is that a traditional isolation technics is widely used in fields such as chemical industry, environmental protection.It is one of core of whole process that desorption in the adsorption process reclaims.Traditional desorption method has water vapour, hot gas desorption, the transformation desorption, and new desorption methods such as electrothermal way, oxidation reclaiming process, ultrasonic regeneration method have appearred again in solvent exchange in recent years
[1,2]Water vapour, hot gas desorption method, be applicable to low-molecular-weight hydrocarbon and the organic saturated charcoal of aromatic series that the desorption boiling point is lower, the water vapour heat content is high and be easy to get, desorption economy and security are better, but for the material desorption ability of higher a little less than, need the long desorption cycle, easily cause the corrosion of system, the raising of system material performance requirement; Water content is higher in the material that reclaims, the secondary pollution problem that also has condensed water, desorb can influence the quality of regenerant when being easy to the pollutant (as halogenated hydrocarbons) of hydrolysis, the adsorption system behind the steam desorption needs the cool drying of long period, could come into operation once more.Compare with the steam desorb, the condensed water secondary pollution of hot gas desorb seldom, the organic matter water content of recovery low (for the more apparent advantage of water miscible organic matter) is convenient to further refining the recovery, the time of regeneration of adsorbent beds drying, cooling is shorter, and is relatively low to the adsorption system material requirements
[3]The shortcoming of hot gas desorption is that gas heat capacity is less, and the required area of gas heat exchange is relatively large
[4]In addition,, may have certain danger, and the existence of oxygen can influence the quality of recover materials,, increase recovery cost so under the part situation gas oxygen content is had certain requirement in the hot gas regenerative process if directly adopt the hot-air desorb.
The solvent exchange method makes the adsorbent desorb by changing the concentration of absorbed component, emits absorbed component, and solvent is got rid of in heating then, makes adsorbent reactivation, and medicament wash-out and supercritical fluid method of reproduction are its representatives.The medicament elution method is applicable to desorption high concentration, lower boiling organic matter, utilizes the product characteristics of easy desorption under certain condition, makes adsorbate and suitable chemicals reaction, reaches the purpose of regenerated carbon.This method can reclaim utility sometimes from regenerated liquid, regenerative operation can carry out in adsorption tower, the active carbon loss is less, but used organic solvent price height, some has toxicity, can bring secondary pollution, and is with strong points, it is not thorough to regenerate, can stop up the micropore of active carbon, influence the recovery rate of absorption property, repeatedly the absorption property of regeneration back active carbon obviously reduces.The supercritical fluid method of reproduction utilizes supercritical fluid as solvent, be dissolved among the supercritical fluid being adsorbed on organic pollution on the active carbon, utilize the relation of fluid properties and temperature and pressure again, organic matter is separated with supercritical fluid, reach the purpose of regeneration.This method operating temperature is low, does not change the original structure of physics, chemical property and the active carbon of adsorbate, and active carbon is without any loss, help the utilization again of adsorbate, cut off secondary pollution, and realize the serialization of operation, reclaim equiment takes up an area of little, energy efficient.But the organic pollution that this method is studied is very limited, the popularity that this technology difficult of proof is used
[3]Electric heating desorption method, Fabuss and Dubois utilized the electric conductivity of sorbing material in 1970, the adsorbent after absorption is saturated applies electric current, utilized Joule effect to give birth to heat, for desorb provides energy.At present, electric current has two kinds of producing methods: electrode directly produces electric current and electromagnetic induction produces electric current indirectly.Compare with traditional alternating temperature desorption method, the regeneration gas flow can reduce 10%～20%.But heat spot can appear in the contact-making surface at granular activated carbon when directly heating, and influences the temperature controlling of adsorption bed, is difficult to amplify, and is being still waiting further further investigation aspect arrangement of electrodes connection and the insulation in addition
[5,6]Other desorption method also has microwave desorption method, ultrasonic wave etc., all has development potentiality preferably on operation principle, is also waited to do by a lot of work but will reach the engineering application.
[1]Lingai?Luo，David?Ramirez，Mark?J.Rood，etc. Adsorption?and?electrothermal?desorption?oforganic?vapors?using?activated?carbon?adsorbents?with?nov
[2]J.F.Nastaj，B.Ambrozek，J.Rudnicka.Simulation?studies?of?a?vacuum?and?temperature?swingadsorption?process?for?the?removal?of?VOC?from?waste?air?streams.InternationalCommunication?in?Heat?and?Mass?Transfer.2006，33(1)：80-86
[3]E.J.Mezey，S.T.Dinovo.Adsorbent?Regeneration?and?Gas?Separation?Utilizing?MicrowaveHeating.US?Patent?4322394(1980).
[4]Leslie?R.Flink，Bryce?J.Fox，Mary?K.Witzel.Vapor?Recovery?Method?and?Apparatus.UnitedStates：4480393，1984，11，6
[5]Feng?Dong?Yu.Lingai?Luo，Georges?Grevillot.Electrothermal?swing?adsorption?of?toluene?onan?activated?carbon?monolith?Experiments?and?parametric?theoretical?study.ChemicalEngineering?and?Processing.2007，46(1)：70-81.
[6]Patrick?D.Sullivan，Mark?J.Rood，M.ASCE，Katherine?D.Dombrowski，et?al.Capture?ofOrganic?Vapors?Using?Adsorption?and?Electrothermal?Regeneration.J?Environ?Eng.2004，130(3)：258-267。
Summary of the invention
The object of the present invention is to provide a kind of energy consumption low, the inert gas consumption is low, and the recovery time is shorter, recover materials quality better, the adsorbent bed circulating desorption distributary recovery regeneration process of less secondary pollution and device thereof.
Below so that the description of having adopted absorbing, recovering and purifying organic technology in the complete exhaust of inventing the desorption and regeneration method that proposes is illustrated summary of the invention.
The adsorbent bed circulating desorption distributary recovery regeneration process that the present invention proposes carries out continuous adsorption, desorption process by the absorber alternate cycles that contains adsorbent more than two, realizes continuous absorption, desorption and the recovery of organic matter in the exhaust, and concrete steps are as follows:
(1) contains organic exhaust successively by filter 1, spark arrester 2, under the control of sequencing valve and main air blower 17, enter wherein absorber,, then finish organic adsorption process in the exhaust when absorber arrives breakthrough point;
(2) finish the keying control of absorber by sequencing valve after the absorption, this absorber and absorption inlet, outlet system are isolated, simultaneously and flow detector (18), formation such as circulating fan (19) and flow type calorifier (21) hot gas circulation desorption loop;
(3) to feed replenishing source of the gas 30 in the closed circuit described in the step (2), the oxygen-containing gas in the gas heat cycles loop being replaced, making that oxygen content is lower than 10% in the closed circuit; Start flow type calorifier 21 and circulating fan 19, the flow of circulating fan 19 is the 20-120% of main air blower 17 flows, and gas is heated to design temperature by heater 21 in the closed circuit, and the organic matter in the adsorbent is carried out desorption;
(4) rising the zero hour with the cocycle heating, in the setting period, keeping air bleeding valve 9 or 10 to be in opening, exclusive segment expanded by heating gas.
(5) when gas in the closed circuit described in the step (2) begin the heating or the circulation be heated to setting-up time after, start refrigerant and condenser fan, the part circulation is rich in organic gas by the shunting circuit condensation after adding thermal desorption, to be the part air-flow enter heat exchanger (23) by the somewhere pipeline by-pass shunt of circulating fan 19 outlets and 20 on valve through valve 22 tentatively cools off, split ratio is 1%-50%, and the partial organic substances condensate liquid that obtains reclaims by the heat exchanger tapping line that valve 29 is set; The preliminary cooled gas that heat exchanger (23) is discharged then enters further condensation of condenser (27), and the organic matter condensate liquid that obtains after the condensation reclaims by the condenser tapping line that valve 28 is set;
(6) gas of the uncooled part in step (5) condensation process is successively by condenser fan (25), traffic probe instrument (24), Returning heat-exchanger (23) condensation for the treatment of that entered shunting circuit via valve 22 is reclaimed air-flow and heated again, and comes back to the recyclegas heating circuit by valve 26;
(7) after arriving the setting desorption time, the low-temperature receiver of closed gas flow heater (21), circulating fan (19), condenser fan (25) and condenser (27) successively, control system makes absorber withdraw from detachment status by sequencing valve, absorber behind this desorption is prepared the adsorption process that enters following one-period after cooling.
Among the present invention, described additional source of the gas adopts low oxygen content gas, as nitrogen, carbon dioxide or in the inert gases such as combustion product gases after purifying any.
The adsorbent bed circulating desorption distributary recovery regeneration device that the present invention proposes, by filter 1, spark arrester 2, absorber, determination of oxygen content probe 3, main air blower 17, recyclegas gauge 18, hot gas circulating fan 19, flow type calorifier 21, shunting gas heat-exchanger 23, shunting gas flowmeter 24, shunting condensed gas blower fan 25, shunting gas condenser 27, replenish source of the gas 30 and corresponding pipeline, sequencing valve and control system are formed by connecting, its structure such as absorber quantity are that 2 o'clock structure is shown in Figure 1.Wherein, filter 1 links to each other with spark arrester 2, and spark arrester 2 connects absorber one end, the absorber other end by sequencing valve connection main air blower 17 by sequencing valve; The sequencing valve 7 in parallel and the interflow head of 8 valve groups, recyclegas gauge 18, circulating fan 19, circulating current heater 21 and sequencing valve 13 in parallel link to each other successively with 14 valve mix flow heads, and the opposite side of the sequencing valve group of two groups of parallel connections does not merge joint and is connected to formation gas heat cycles loop, 2 absorber two ends respectively; Shunting gas heat-exchanger 23, shunting gas condenser 27, shunting condensed gas blower fan 25 link to each other successively with shunting gas flowmeter 24, are connected to sequencing valve or other type valves 22 and sequencing valve or other type valves 26 two ends, constitute shunting condensation loop; Replenishing source of the gas 30 is connected between circulating current heater 21 and absorber clean gas outlet end valve 13 or 14 by sequencing valve 31; Determination of oxygen content probe 3 links to each other with unidirectional stop valve 4, is connected between spark arrester 2 and the absorber gas access to be clean; Determination of oxygen content probe 3, each sequencing valve, main air blower 17, recyclegas flow instrument 18, hot gas circulating fan 19, flow type calorifier 21, shunting gas flowmeter 24, shunting condensed gas blower fan 25 and condenser refrigerant switch be connection control system respectively.
Among the present invention, in parallel between the described absorber.
Among the present invention, desorption process adopts band shunting circulation gas circuit mode.The gas of heating enters absorber it is carried out desorption.In the gas heat cycles after the regular hour, part circulation adds is rich in organic gas behind the thermal desorption and enters cools down by the by-pass shunt system, obtaining the partial organic substances cooling fluid reclaims, remainder gas enters the further condensation of condenser, the organic matter condensate liquid that obtains after the condensation reclaims, uncooled portion gas in the condensation enters heat exchanger heats, comes back to the circulating current heating systems.After arriving the setting desorption time, control system makes absorber withdraw from detachment status by the process control valve, after cooling, prepares the adsorption process that enters following one-period.
The present invention has following benefit by the desorb that low oxygen-containing gas closed circuit circulatory system carries out adsorbent: (1) closed cycle has improved the dividing potential drop of organic gas in the gas phase effectively under the situation that does not influence rate of heat transfer, help condensation separation, (2) because closed cycle, controlled the total oxygen in the loop gas, make that the possibility of organic matter generation chemical change reduces greatly in the regenerative process, it is better to reclaim organic quality, and (3) low to be contained the oxygen total amount and guaranteed security of system.
The present invention can reduce condensation process equipment input and energy consumption greatly by the mode that adopts the shunting condensation, effectively improves the economy that technology is reclaimed in regeneration.
The present invention can further reduce the energy consumption of gas heating and cooling in the shunting condenser system by treating to set heat exchanger between condensed gas and condensation final vacuum, thereby reduces the cost that organic matter reclaims.
The present invention can increase under few situation in the system equipment expense by improving the mode of desorption gas temperature, carries out the organic recovery of some highers (as the DMAC of 166 ℃ of boiling points).
The present invention compares with the steam desorb, and refrigeration costs is low, essentially no secondary pollution, and the organic matter water content of recovery low (for the more apparent advantage of water miscible organic matter) is convenient to further refining the recovery, and the time dry, that cooling is required of regeneration simultaneously is shorter.
The present invention is by the recyclegas thermal desorption, the process combined mode is reclaimed in shunting gas heat exchange and condensation, the recovery purpose of finishing adsorbent bed desorption adsorbate that can be continuous automatically, under the prerequisite that guarantees the recovery yield, improved the efficiency of energy utilization of desorption process effectively, control simultaneously the scale of investment of cooling system effectively, solved the safety problem of hot gas desorb, the recovery organic matter purity height that obtains simultaneously, follow-up refining expense is low, has expanded chemical adsorbing separation, has adsorbed the range of application that reclaims gaseous contaminant.The present invention can be used for chemical adsorbing separation, gaseous contamination purification and organic solvent and reclaims occasion, is particularly suitable for water-soluble, facile hydrolysis organic solvent tail gas recycle, and it reclaims yield greater than 90%.
Description of drawings
Fig. 1 is a process chart of the present invention.
Number in the figure: 1 is filter, and 2 is spark arrester, and 3 are the determination of oxygen content probe, 4 is unidirectional stop valve, and 5,6,7,8,9,10,13,14,15,16,20,22,26,28,29,31 are respectively sequencing valve and other types valve, and 11,12 are respectively absorber, 17 is main air blower, and 18 is the recyclegas gauge, and 19 is circulating fan, 21 is the circulating current heater, 23 are the shunting gas heat-exchanger, and 24 are the shunting gas flowmeter, and 25 is blower fan, 27 is condenser, and 30 for replenishing source of the gas.
The specific embodiment
Further specify the present invention below by embodiment.5000m
3/ h dimethylbenzene exhaust-gas treatment reclaims.
Embodiment 1:
Following each parts are connected by mode shown in Figure 1, and the person skilled in art all can smooth implementation.Apparatus of the present invention adopt the AF5-N type by a pneumatic filter, a spark arrester adopts net type HGS07, two absorbers that are filled with adsorbent adopt the CAU5-G type, a main air blower adopts the BF9-26NO5A type, a heat exchanger adopts the AAE-2-B type, a circulating current heater adopts the GL-5 type, a gas condenser adopts the TLS-10-12-400 type, a circulating fan adopts formations such as BF9-264A type, replenish source of the gas 31 and adopt nitrogen, determination of oxygen content probe 3 adopts the TB2A zirconium oxide-oxygen probe, automatic control system adopts the PLC cyclelog, and the model of sequencing valve is the pneumatic dish valve of KVD.
In system when operation, after the exhaust that contains toluene is removed particle by filter 1, enter follow-up reclaiming system through spark arrester 2, be that example illustrates technical process with absorber 11 below.
Automatic control system is by the control to sequencing valve and main air blower 17, determine that the gas flow process in the system pipeline flows to, promptly sequencing valve 5, sequencing valve 15 are opened at this moment, sequencing valve 7, sequencing valve 9, sequencing valve 13 are in closed condition, the organic exhaust gas that contains toluene is discharged after by absorber 11 adsorption cleanings, when absorber 11 during, then finish the adsorption process of toluene in the exhaust near breakthrough point.
In the regeneration stage, automatic control system switches to reproduced state by the control to sequencing valve with absorber 11.Promptly sequencing valve 5, sequencing valve 15 are closed at this moment, and sequencing valve 9, sequencing valve 13, sequencing valve 31 are opened.By the oxygen content in the determination of oxygen content probe 3 mensuration closed circuits, with nitrogen as a supplement source of the gas 30 feed in the closed circuits, oxygen-containing gas in the closed circuit is replaced, when the oxygen content percent by volume is lower than 10% in determination of oxygen content is popped one's head in 3 display pipeline, close sequencing valve 9 and sequencing valve 31, open sequencing valve 7, sequencing valve 20.
ON cycle blower fan 19, start flow type calorifier heating agent switch, the formation stripping gas heats and circulates, the flow of circulating fan 19 be controlled at respectively main air blower 17 flows 20%～40%, 50%-70%, 80%-120%, after waiting to reach the design temperature certain hour, open the refrigerant switch of sequencing valve 22, sequencing valve 26, condenser 27, suitably close flow control valve 20.
The gas that reaches design temperature carries out desorb by pipeline to the adsorbent in the absorber 11, the gas that high concentration after the desorb is rich in toluene is partly shunted and is entered the condensation loop, split ratio is respectively 1%-10%, 20%-25%, 40%-50%, after obtaining to a certain degree cooling by heat exchanger 23, obtain the direct tieback of partial organic substances cooling fluid, the remainder toluene gas enters further condensation in the condenser 27, toluene becomes liquid from condensation of gas in condenser 27 after, be transported to the solvent storage tank by sequencing valve 28 discharges, directly reclaim.Condensed remainder gas is successively by condenser fan 25, traffic probe instrument 24, Returning heat-exchanger 23 heating again, heat up after containing the toluene gas heat exchange by the high concentration after heat exchanger 23 and the desorb, get back to the circulating current heating circuit, repeat to shunt condensation, after arriving the setting desorption time, control system makes absorber 11 withdraw from the desorption stage by closing sequencing valve, prepares the adsorption process that enters following one-period.
Absorber 11 can drop into the adsorption operations of following one-period by cooling after desorb was finished.Wherein, the volume in gas pipeline loop be respectively adsorbent filling volume 2-5 doubly, 5-10 doubly, 15-20 doubly.
When absorber 11 is finished adsorption process, automatic control system is by the control to sequencing valve and main air blower 17, the gas flow process that redefines in the system pipeline flows to, be that sequencing valve 6, sequencing valve 16 are opened, sequencing valve 8, sequencing valve 10, sequencing valve 14 are in closed condition, make pending gas enter adsorption process by absorber 12.Absorber 11 and 12 absorption, desorb blocked operation can be realized continuous absorption, desorption and the reclaimer operation of organic matter in the exhaust.
Claims (2)
1. adsorbent bed hot gas circulating desorption distributary recovery regeneration process, it is characterized in that carrying out continuous adsorption, desorption process by the absorber alternate cycles that contains adsorbent more than two, realize continuous absorption, desorption and the recovery of organic matter in the exhaust, concrete steps are as follows:
(1) contains organic exhaust successively by filter (1), spark arrester (2), under the control of sequencing valve and main air blower (17), enter wherein absorber,, then finish organic adsorption process in the exhaust when absorber arrives breakthrough point;
(2) finish the keying control of adsorbent bed by sequencing valve after the absorption, this absorber and absorption inlet, outlet system are isolated, simultaneously and flow detector (18), formation such as circulating fan (19) and flow type calorifier (21) hot gas circulation desorption loop;
(3) replenish source of the gas (30) to feeding in the closed circuit described in the step (2), oxygen-containing gas in the gas heat cycles loop is replaced, and by open valve (9) or (10) discharging, make that oxygen content is lower than 10% in the closed circuit, start flow type calorifier (21) and circulating fan (19), the flow of circulating fan (19) is the 20-120% of main air blower (17) volume flow;
(4) rising the zero hour with the cocycle heating, setting certain period maintenance air bleeding valve (9) or (10) and be in opening, discharge section expanded by heating gas, the time is 0-5 hour.
(5) air communication in the closed circuit described in the step (2) is crossed flow type calorifier (21) and is heated to design temperature, and the organic matter in the adsorbent is carried out desorption; After heat cycles begins or arrives setting-up time, start refrigerant and condenser fan, the part circulation is rich in organic gas by the shunting circuit condensation after adding thermal desorption, to be the part air-flow enter heat exchanger (23) by the somewhere pipeline by-pass shunt of circulating fan 19 outlets and 20 on valve through valve 22 tentatively cools off, split ratio is 1%-50%, and the partial organic substances condensate liquid that obtains reclaims by the heat exchanger tapping line that valve 29 is set; The preliminary cooled gas that heat exchanger (23) is discharged then enters further condensation of condenser (27), and the organic matter condensate liquid that obtains after the condensation reclaims by the condenser tapping line that valve 28 is set;
(6) gas of the uncooled part in step (5) condensation process is successively by condenser fan (25), traffic probe instrument (24), Returning heat-exchanger (23) condensation for the treatment of that entered shunting circuit via valve 22 is reclaimed air-flow and heated again, and comes back to the recyclegas heating circuit by valve 26;
(7) after arriving the setting desorption time, the low-temperature receiver of closed gas flow heater (21), circulating fan (19), condenser fan (25) and condenser (27) successively, control system makes absorber withdraw from detachment status by sequencing valve, absorber behind this desorption is prepared the adsorption process that enters following one-period after cooling;
Wherein: the volume in gas pipeline loop is 2-20 a times of adsorbent filling volume.
2. an adsorbent bed hot gas circulating desorption distributary as claimed in claim 1 reclaims the regenerating unit that technology constitutes, by filter (1), spark arrester (2), absorber, determination of oxygen content probe (3), main air blower (17), recyclegas gauge (18), hot gas circulating fan (19), flow type calorifier (21), shunting gas heat-exchanger (23), shunting gas flowmeter (24), shunting condensed gas blower fan (25), shunting gas condenser (27), replenish source of the gas (30) and corresponding pipeline, sequencing valve and control system are formed by connecting, it is characterized in that filter (1) links to each other with spark arrester (2), spark arrester (2) connects absorber one end by sequencing valve, the absorber other end connects main air blower (17) by sequencing valve; The interflow head of interflow head, recyclegas gauge (18), circulating fan (19) and the circulating current heater (21) of the sequencing valve group of some in parallel (equating with absorber quantity), another sequencing valve of organizing the some of parallel connection (equating with absorber quantity) links to each other successively, and the opposite side of the sequencing valve group of two groups of parallel connections does not simultaneously merge joint and is connected to the suitable formation gas heat cycles loop, absorber air-flow import and export two ends of corresponding quantity respectively; The passage 2 of the passage 1 of valve (22), shunting gas heat-exchanger (23), shunting gas condenser (27), shunting condensed gas blower fan (25), shunting gas flowmeter (24), shunting gas heat-exchanger (23) links to each other successively with valve (26), be connected to the valve (20) during circulating fan (19) and hotline heater (21) are taken in the gas heat cycles loop or the pipeline section of other type, the two ends of pipe fitting, constitute shunting condensation loop; Replenishing source of the gas (30) is connected between the sequencing valve (13) or (14) of flow type calorifier (21) and absorber interface by valve (31); Determination of oxygen content probe (3) links to each other with unidirectional stop valve (4), is connected between the sequencing valve (9) or (10) of spark arrester (2) and absorber interface; Determination of oxygen content probe (3), each sequencing valve, main air blower (17), recyclegas flow instrument (18), hot gas circulating fan (19), flow type calorifier (21), shunting gas flowmeter (24), shunting condensed gas blower fan (25), condenser refrigerant system etc. are connection control system respectively, and absorber is 2-10.
(3) a kind of adsorbent bed circulating desorption distributary as claimed in claim 1 reclaims the regenerating unit that technology constitutes, and the gas that valve 9 or 10 initial periods at the circulation desorption give off the heating dilation is set.
(4) a kind of adsorbent bed circulating desorption distributary as claimed in claim 1 reclaims the regenerating unit that technology constitutes, and regulates the air circulation of different phase in regenerative process by means such as fan frequency conversion and valve regulated.
(5) a kind of adsorbent bed circulating desorption distributary as claimed in claim 1 reclaims the regenerating unit that technology constitutes, and its thermal regeneration process constitutes different closed circuits with the condensation removal process, and the condensation loop is the shunting circuit in thermal regeneration loop.
(6) a kind of adsorbent bed circulating desorption distributary as claimed in claim 1 reclaims the regenerating unit that technology constitutes, and is provided with the heat-exchanger rig that enters the condenser system air-flow and get rid of the condenser system air-flow in the condensation loop
(7) a kind of adsorbent bed circulating desorption distributary as claimed in claim 1 reclaims the regenerating unit that technology constitutes, and its condensation adds freezing liquid condensation combination collocation by air-cooled or water-cooled and forms.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005021861A (en) * | 2003-07-02 | 2005-01-27 | Nippo Kagaku Kk | Alkyl iodide recovery method and alkyl iodide recovery apparatus |
| CN101081361A (en) * | 2007-06-28 | 2007-12-05 | 同济大学 | Adsorbent bed circulating desorption distributary recovery regeneration process and device thereof |
-
2010
- 2010-03-31 CN CN 201010137405 patent/CN102205235A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005021861A (en) * | 2003-07-02 | 2005-01-27 | Nippo Kagaku Kk | Alkyl iodide recovery method and alkyl iodide recovery apparatus |
| CN101081361A (en) * | 2007-06-28 | 2007-12-05 | 同济大学 | Adsorbent bed circulating desorption distributary recovery regeneration process and device thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
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| CN110548361A (en) * | 2018-05-31 | 2019-12-10 | 中国船舶重工集团公司第七一一研究所 | Recovery system and recovery method of organic waste gas |
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