CN101081361A - Adsorbent bed circulating desorption distributary recovery regeneration process and device thereof - Google Patents
Adsorbent bed circulating desorption distributary recovery regeneration process and device thereof Download PDFInfo
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Abstract
The present invention belongs to the field of chemical separating and environment protecting technology, and is especially circular desorbing, shunting, recovering and regenerating process in an adsorbing bed and the apparatus. The technological process includes circular desorbing on hot gas in an adsorbing bed, and by-pass heat exchange and condensing recovery of partial desorbed gas flow. The present invention has the advantages low power consumption, low cost and high purity of the recovered organic matter, and is especially suitable for use in chemical adsorbing and separating process, contaminated gas purifying, organic solvent recovery, etc.
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 in the hot gas regenerative process gas oxygen content is had certain requirement 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?novelmorphologies.Carbon.2006，44(13)：2715-2723)
[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] Ceng Huaxing. charcoal absorption carbon disulfide and microwave desorb research. University Of Nanchang's master thesis, 2006
[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，etal.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 short, 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) to feed replenishing source of the gas 30 in the closed circuit described in the step (1), 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 heated air circulating fan 19, the flow of circulating fan 19 is the 20-120% of main air blower 17 flows;
(3) gas in the closed circuit in the step (2) is heated to design temperature by heater 21, the organic matter in the adsorbent is carried out desorption; When gas heat cycles in the closed circuit behind setting-up time, the part circulation is rich in organic gas employing shunting condensation after adding thermal desorption, enter heat exchanger 23 coolings by the by-pass shunt system, obtain the partial organic substances cooling fluid and directly reclaim, split ratio is 1%-50%; Remainder gas then enters condenser 27 further condensations, and the organic matter condensate liquid that obtains after the condensation reclaims;
(4) the uncooled portion gas in step (3) condensation by condenser fan 25, traffic probe instrument 24, Returning heat-exchanger 23 heating again, comes back to gas heat cycles loop successively;
(5) after arriving the setting desorption time, control system makes absorber withdraw from detachment status by sequencing valve, after air-cooled, prepares the adsorption process that enters following one-period;
Wherein: the volume in gas pipeline loop is 2-20 a times of adsorbent filling volume.
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, circulating current heater 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 is as 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; Recyclegas gauge 18, circulating fan 19 and circulating current heater 21 link to each other successively, are connected to the absorber two ends and constitute gas heat cycles loop; 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 22 and sequencing valve 26 two ends, constitute shunting condensation loop; Replenishing source of the gas 30 is connected between circulating current heater 21 and the absorber 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; Determination of oxygen content probe 3, each sequencing valve, main air blower 17, recyclegas flow instrument 18, hot gas circulating fan 19, shunting gas flowmeter 24, shunting condensed gas blower fan 25 be connection control system respectively, and absorber is 2-10.
Among the present invention, in parallel between the described absorber.
Among the present invention, desorption process adopts band shunting circulation gas circuit mode.Gas is heated to and enters absorber after the uniform temperature 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 air-cooled, 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 85%.
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 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 toluene waste gas is handled and is reclaimed.
Embodiment 1-embodiment 3:
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 the 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 gas heater 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, obtaining the partial organic substances cooling fluid directly reclaims, 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 air-flow heat cycles loop, 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.
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 (5)
1, a kind of adsorbent bed 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) replenish source of the gas (30) to feeding in the closed circuit described in the step (1), oxygen-containing gas in the gas heat cycles loop is replaced, make that oxygen content is lower than 10% in the closed circuit, start heated air circulating fan (19), the flow of circulating fan (19) is the 20-120% of main air blower (17) flow;
(3) gas in the closed circuit described in the step (2) is heated to design temperature by heater (21), organic matter in the adsorbent is carried out desorption, after gas is heated to setting-up time in the closed circuit, the part circulation is rich in organic gas employing shunting condensation after adding thermal desorption, enter heat exchanger (23) cooling by the by-pass shunt system, obtain the partial organic substances cooling fluid and reclaim, split ratio is 1%-50%; Remainder gas then enters further condensation of condenser (27), and the organic matter condensate liquid that obtains after the condensation reclaims;
(4) the uncooled portion gas in step (3) condensation by condenser fan (25), traffic probe instrument (24), Returning heat-exchanger (23) heating again, comes back to gas heat cycles loop, repeating step (3) successively;
(5) after arriving the setting desorption time, control system makes absorber withdraw from detachment status by sequencing valve, after air-cooled, prepares the adsorption process that enters following one-period;
Wherein: the volume in gas pipeline loop is 2-20 a times of adsorbent filling volume.
2, according to claim 1 adsorbent bed circulating desorption distributary recovery regeneration process is characterized in that described additional source of the gas adopts low oxygen content gas.
3, according to claim 2 adsorbent bed circulating desorption distributary recovery regeneration process, it is characterized in that described low oxygen content gas be nitrogen, carbon dioxide or purify after combustion product gases in any.
4, a kind of adsorbent bed circulating desorption distributary recovery regeneration device as claimed in claim 1, 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), circulating current heater (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; Recyclegas gauge (18), circulating fan (19) and circulating current heater (21) link to each other successively, are connected to the absorber two ends and constitute gas heat cycles loop; 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 (22) and sequencing valve (26) two ends, constitute shunting condensation loop; Replenishing source of the gas (30) is connected between circulating current heater (21) and the absorber 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; Determination of oxygen content probe (3), each sequencing valve, main air blower (17), recyclegas flow instrument (18), hot gas circulating fan (19), shunting gas flowmeter (24), shunting condensed gas blower fan (25) be connection control system respectively, and absorber is 2-10.
5, adsorbent bed circulating desorption distributary recovery regeneration device according to claim 4 is characterized in that between the described absorber in parallel.
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| WO2009105967A1 (en) * | 2008-02-29 | 2009-09-03 | Su Qingquan | An adsorption device and a method for regenerating the adsorbent |
| CN102205235A (en) * | 2010-03-31 | 2011-10-05 | 羌宁 | Method and apparatus for circulating, desorbing, shunting, recovering, and reclaiming hot gas by using adsorption bed |
| CN103272455A (en) * | 2013-06-14 | 2013-09-04 | 泉州市天龙环境工程有限公司 | Device and method for recycling organic solvents from painting waste gas |
| CN104649448A (en) * | 2010-08-11 | 2015-05-27 | 东洋纺株式会社 | Waste water treatment system |
| CN105126531A (en) * | 2015-07-22 | 2015-12-09 | 同济大学 | Device of increasing adsorption bed thermal-circular gas desorption regeneration efficiency and method thereof |
| CN105233621A (en) * | 2015-10-10 | 2016-01-13 | 王新洲 | Novel volatile organic compounds environmental-protection governance recovery method and device |
| CN105457445A (en) * | 2015-12-18 | 2016-04-06 | 广州朗洁环保科技有限公司 | Energy-saving condensation organic waste gas recycling device |
| CN107824007A (en) * | 2017-11-28 | 2018-03-23 | 上海亿景能源科技有限公司 | The regenerative system of heating carrier is used as by the use of waste gas itself |
| CN107998877A (en) * | 2017-11-28 | 2018-05-08 | 江苏科威环保技术有限公司 | More component organic exhaust gas recycle abatement technique |
| CN108865249A (en) * | 2018-07-20 | 2018-11-23 | 北京欧美中科学技术研究院 | A kind of intermediate oil desulfurizer |
| CN109158085A (en) * | 2018-10-30 | 2019-01-08 | 南京兆博环保科技有限公司 | A kind of dry cooling device and method of active-carbon bed safety |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2009105967A1 (en) * | 2008-02-29 | 2009-09-03 | Su Qingquan | An adsorption device and a method for regenerating the adsorbent |
| CN101518706B (en) * | 2008-02-29 | 2011-11-09 | 苏庆泉 | Adsorption device and adsorbent regeneration method |
| CN102205235A (en) * | 2010-03-31 | 2011-10-05 | 羌宁 | Method and apparatus for circulating, desorbing, shunting, recovering, and reclaiming hot gas by using adsorption bed |
| CN104649448A (en) * | 2010-08-11 | 2015-05-27 | 东洋纺株式会社 | Waste water treatment system |
| CN103272455A (en) * | 2013-06-14 | 2013-09-04 | 泉州市天龙环境工程有限公司 | Device and method for recycling organic solvents from painting waste gas |
| CN103272455B (en) * | 2013-06-14 | 2015-02-04 | 泉州市天龙环境工程有限公司 | Device and method for recycling organic solvents from painting waste gas |
| CN105126531A (en) * | 2015-07-22 | 2015-12-09 | 同济大学 | Device of increasing adsorption bed thermal-circular gas desorption regeneration efficiency and method thereof |
| CN105126531B (en) * | 2015-07-22 | 2017-12-26 | 同济大学 | A kind of devices and methods therefor for improving adsorbent bed circulation of hot gases desorption and regeneration efficiency |
| CN105233621A (en) * | 2015-10-10 | 2016-01-13 | 王新洲 | Novel volatile organic compounds environmental-protection governance recovery method and device |
| CN105457445A (en) * | 2015-12-18 | 2016-04-06 | 广州朗洁环保科技有限公司 | Energy-saving condensation organic waste gas recycling device |
| CN107824007A (en) * | 2017-11-28 | 2018-03-23 | 上海亿景能源科技有限公司 | The regenerative system of heating carrier is used as by the use of waste gas itself |
| CN107998877A (en) * | 2017-11-28 | 2018-05-08 | 江苏科威环保技术有限公司 | More component organic exhaust gas recycle abatement technique |
| CN108865249A (en) * | 2018-07-20 | 2018-11-23 | 北京欧美中科学技术研究院 | A kind of intermediate oil desulfurizer |
| CN109158085A (en) * | 2018-10-30 | 2019-01-08 | 南京兆博环保科技有限公司 | A kind of dry cooling device and method of active-carbon bed safety |
| CN109759037A (en) * | 2019-01-25 | 2019-05-17 | 安徽国孚凤凰科技有限公司 | A kind of desorption apparatus and method of silica gel purification Reclaimed Base Oil |
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