CN103585854A - Technology for recovering and processing organic exhaust gas by activated carbon adsorption and N2 desorption - Google Patents
Technology for recovering and processing organic exhaust gas by activated carbon adsorption and N2 desorption Download PDFInfo
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- CN103585854A CN103585854A CN201310520571.3A CN201310520571A CN103585854A CN 103585854 A CN103585854 A CN 103585854A CN 201310520571 A CN201310520571 A CN 201310520571A CN 103585854 A CN103585854 A CN 103585854A
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Abstract
The invention provides a technology for recovering and processing organic exhaust gas by activated carbon adsorption and N2 desorption. The technology comprises the following steps: organic exhaust gas is pretreated by a coil-cooling filter; the organic exhaust gas which has been pretreated is then sent into a first activated carbon adsorption tank for adsorption; after adsorption of the first activated carbon adsorption tank, the system enters a desorption stage, and a second activated carbon adsorption tank enters an adsorption stage; the desorbed organic exhaust gas is condensed and then recovered, and after desorption of the system, the first activated carbon adsorption tank is cooled to a certain temperature, and back-purging is conducted on the first activated carbon adsorption tank, and the temperature drops to normal temperature after back-purging so as to use the exhaust gas in the next circulation; and the first activated carbon adsorption tank and the second activated carbon adsorption tank recycle and alternate the above steps. By the adoption of the technology, secondary pollution will not be caused; energy consumption is low; and the quality of recovered organic solvents is pure.
Description
[technical field]
The present invention relates to a kind of charcoal absorption, N
2the technique of desorption recycling organic exhaust gas.
[background technology]
The VOCs saturated vapor pressure that is a class boiling point under 50 ℃～260 ℃, room temperature surpasses the volatile organic compound of 133.3Pa, and health and ecological environment are had to very large harm.How effectively this class organic exhaust gas of recycling and administration, can not only avoid environmental pollution, and turn waste into wealth, and has reduced the cost of investment of enterprise, realizes the doulbe-sides' victory of social benefit and economic benefit.
In organic solvent recovery method, being still of being most widely used be take " charcoal absorption-water vapour desorption-condensation is reclaimed " as main at present, yet this method exists more problem in actual applications.Developed in recent years a kind of organic exhaust gas absorption method that nitrogen is heat carrier of take.
The Chinese patent that for example application number is 200810114892.2, a kind of active carbon fiber organic gas recovery method and system that nitrogen is desorption medium of take disclosed, it take the fixed-bed adsorber that NACF is adsorbent, adopt hot nitrogen desorption, simultaneously recycling organic exhaust gas and nitrogen; Thisly using anti-flammability gas and replace steam and efficiently solve as the desorption recovery process of heat carrier the variety of problems of bringing because of steam desorption, replaced to a certain extent charcoal absorption-water vapour desorption absorption method.But, because the thermal capacity of anti-flammability gas is less than steam, the heat exchange area that causes air heat clearing house to need is relatively large, and these volatile organic gas are reclaimed in condensation, required condensation temperature is lower, in addition, the gas that desorption desorbs still contains the organic exhaust gas of higher concentration after condensation, and these make this recovery process on engineering application, have certain limitation.
Because VOCs gas boiling point is low, volatile, saturated vapor pressure surpasses 133.3Pa at normal temperatures, and heat transmission equipment is had high input, and energy consumption is high, and condensed gas still contains the organic exhaust gas of higher concentration.Prior art is mainly to adopt the condensation of large area heat exchanger, and in desorption condensation, reclaim a second adsorption device of end increase and carry out the condensed gas of adsorption treatment, this not only makes technique more complicated and control difficulty and strengthen, and has also increased the cost of investment of enterprise simultaneously.
[summary of the invention]
The technical problem to be solved in the present invention, is to provide a kind of charcoal absorption, N
2the technique of desorption recycling organic exhaust gas, this technique can not cause secondary pollution, and energy consumption is low, and the organic solvent quality reclaiming is purer.
The present invention is achieved in that
A kind of charcoal absorption, N
2the technique of desorption recycling organic exhaust gas, described processing step is as follows:
Step 10, organic exhaust gas enter the cold filter of table by main air blower and carry out pretreatment, and organic exhaust gas after pretreatment is sent into the first absorbent charcoal adsorption tank again and adsorbed;
Step 20, when the first absorbent charcoal adsorption tank absorption arrives a default breakthrough point, close and open corresponding valve, make the first absorbent charcoal adsorption tank enter the desorption system stage, the second absorbent charcoal adsorption tank enters the adsorption system stage;
N in step 30, use storage nitrogen tank
2replace the gas in the first absorbent charcoal adsorption tank, and the gas displacing is sent back in the cold filter of table, by the second absorbent charcoal adsorption tank, carry out adsorption treatment; When online oxygen analyser detects desorption system oxygen content and is less than 0.5%, control desorption system pressure and after 4～10KPa, close N
2supply with, add N in thermal desorption system pipeline
2the ON cycle desorption blower fan desorption that circulates, the organic exhaust gas parsing divides two parts, the part two-stage condensation equipment of flowing through, a part is through shunt valve, then two parts gas mixes, and mixed gas reheats, and then by circulating fan, is sent in the first absorbent charcoal adsorption tank and is proceeded desorption; After the high-concentration organic waste gas condensation of flowing through after the desorption of two-stage condensation equipment, enter purification system;
After step 40, desorption finish, charcoal layer temperature in the first absorbent charcoal adsorption tank drops to the boiling temperature of VOCs gas when following, close and open corresponding valve, extraction fresh air carries out blowback to be swept, and heats this fresh air to the boiling temperature of VOCs gas simultaneously; The gas purging out enters in the cold filter of table again, by the first absorbent charcoal adsorption tank, carries out adsorption treatment;
Step 50, blowback are swept after end, and intrasystem gas is carried out to condensation cooling, finally by this condensed gas, the charcoal layer in the first absorbent charcoal adsorption tank are lowered the temperature, so that next recycles;
Described the first absorbent charcoal adsorption tank and the above step of the second absorbent charcoal adsorption tank cycle alternation.
Further, in described step 30, the organic exhaust gas of desorption of two-stage condensation equipment of flowing through first carries out tentatively cooling through two-stage condensation front equipment end heat exchanger, can obtain partial organic substances cooling fluid, remaining gas enters further deep layer condensation in B grade condensing unit again, and cooling fluid and condensate recovery liquid enter purification system after intermediate storage tank; Condensed remainder gas is sent back to the desorption that circulates in the first absorbent charcoal adsorption tank again after heating by heater after mixing with the organic exhaust gas of desorption through shunt valve.
Further, in described step 30, partial condensation air quantity (that equipment produces) is respectively 1:1～1:12,80～350 ℃ of desorption system Temperature Settings with the ratio of bypass air quantity (that equipment produces).
Further, in described step 30, when line oxygen conten analyser detects in desorption system oxygen content > 2%, give the alarm, desorption system stops heating and circulation desorption, opens corresponding valve, again carries out nitrogen replacement in system, when oxygen content < 0.5%, reopen desorption manipulation.
Further, described blowback flyback time is desorption time 20%～30%; Described anti-purge air quantity equates with desorption air quantity.
Further, described technique is by PLC control program system whole-process automatic control.
Tool of the present invention has the following advantages:
The present invention adopts partial condensation to reclaim and reverse purging process, not only effectively solved prior art problem, greatly simplified technique, reduced production cost, and overcome the limitation that in desorption removal process in the past, energy consumption is high, heat transmission equipment has high input, the organic matter quality purer feature that has kept hot gas desorption to reclaim; In addition, technological process of the present invention by the detection analyzing and processing to data such as the pressure of system, temperature, oxygen contents, realizes whole-process automatic control by PLC control program system.
[accompanying drawing explanation]
The present invention is further illustrated in conjunction with the embodiments with reference to the accompanying drawings.
Fig. 1 is the process schematic representation of embodiments of the invention.
In figure, each label is expressed as follows:
1, show cold filter; 2, main air blower; 3, Three-way butterfly valve;
A, the first absorbent charcoal adsorption tank; B, the second absorbent charcoal adsorption tank;
A1, A2, A3, A4, the first valve; B1, B2, B3, B4, the second valve;
4, the 3rd valve; 5, the 4th valve; 6, the 5th valve; 7, oil pump; 8, the 6th valve;
9, the 7th valve; 10, oxygen conten analyser; 11, condenser; 12, heater;
13, the 8th valve 14, the 9th valve; 15, circulation desorption blower fan;
16, two-stage condensation equipment; 17, shunt valve; 18, intermediate storage tank.
[specific embodiment]
Refer to shown in Fig. 1, embodiments of the invention are described in detail.
The present invention relates to a kind of charcoal absorption, N
2the technique of desorption recycling organic exhaust gas, described processing step is as follows:
Step 10, organic exhaust gas enter the cold filter of table by main air blower and carry out pretreatment, and organic exhaust gas after pretreatment is sent into the first absorbent charcoal adsorption tank again and adsorbed;
Step 20, when the first absorbent charcoal adsorption tank absorption arrives a default breakthrough point, close and open corresponding valve, make the first absorbent charcoal adsorption tank enter the desorption system stage, the second absorbent charcoal adsorption tank enters the adsorption system stage;
N in step 30, use storage nitrogen tank
2gas in displacement desorption system, and the gas displacing is sent back in the cold filter of table, by the second absorbent charcoal adsorption tank, carry out adsorption treatment; When online oxygen analyser detects desorption system oxygen content and is less than 0.5%, control desorption system pressure and after 4～10KPa, close N
2supply with, add N in thermal desorption system
2, the desorption that then circulates, the organic exhaust gas of desorption divides two parts, the part two-stage condensation equipment of flowing through, a part is through shunt valve, and then two parts gas mixes, and by circulating fan, is sent back in the second absorbent charcoal adsorption tank; After the high-concentration organic waste gas condensation of flowing through after the desorption of two-stage condensation equipment, enter purification system;
After step 40, desorption finish, charcoal layer temperature in the first absorbent charcoal adsorption tank drops to the boiling temperature of VOCs gas when following, close and open corresponding valve, extraction fresh air carries out blowback to be swept, and heats this fresh air to the boiling temperature of VOCs gas simultaneously; The gas purging out enters in the cold filter of table again, by the second absorbent charcoal adsorption tank, carries out adsorption treatment;
Step 50, blowback are swept after end, and intrasystem gas is carried out to condensation cooling, finally by this condensed gas, the charcoal layer in the first absorbent charcoal adsorption tank are lowered the temperature, so that next recycles;
Described the first absorbent charcoal adsorption tank and the above step of the second absorbent charcoal adsorption tank cycle alternation.
Concrete, in described step 30, the organic exhaust gas of desorption of two-stage condensation equipment of flowing through first carries out tentatively cooling through two-stage condensation front equipment end heat exchanger, can obtain partial organic substances cooling fluid, remaining gas enters further deep layer condensation in B grade condensing unit again, and cooling fluid and condensate recovery liquid enter purification system after intermediate storage tank; Condensed remainder gas is sent back to the desorption that circulates in the first absorbent charcoal adsorption tank again after heating by heater after mixing with the organic exhaust gas of desorption through shunt valve.
In described step 30, partial condensation air quantity (by the air quantity of two-stage condensation) is respectively 1:1～1:12,80～350 ℃ of desorption system Temperature Settings with the ratio of bypass air quantity (by the air quantity of shunt valve).In bipolar condensing plant, gas divides two-way to walk: lead up to first preliminary cooling and then deep layer condensation (this is partial condensation); One tunnel without supercooling condensing plant directly by bipolar condensing plant (this is bypass).
In described step 30, when line oxygen conten analyser detects in desorption system oxygen content > 2%, give the alarm, desorption system stops heating and circulation desorption, open corresponding valve, again carry out nitrogen replacement in system, when oxygen content < 0.5%, reopen desorption manipulation.
Described blowback flyback time is desorption time 20%～30%; Described anti-purge air quantity equates with desorption air quantity.Described technique is by PLC control program system whole-process automatic control.
Below in conjunction with specific embodiment, the present invention is further illustrated.
Embodiment
Emphasis is consulted Fig. 1, and processing step is as follows:
One, organic exhaust gas enters the cold filter 1 of table by main air blower 2 and carries out pretreatment, through pretreated organic exhaust gas, is fed to the first absorbent charcoal adsorption tank A and adsorbs, and opens the first valve A2, and purified gas is discharged by exhaust outlet; The second absorbent charcoal adsorption tank B is now in desorption and regeneration stage or stand-by phase, guarantees that cleaning system can continuous operation, do not affect workshop and normally produces;
When two, the first absorbent charcoal adsorption tank A arrives breakthrough point after absorption a period of time, close the first valve A1, A2, open the second valve B1, B2, make the second absorbent charcoal adsorption tank B enter adsorption system, the first absorbent charcoal adsorption tank A enters desorption system.
Three, the first absorbent charcoal adsorption tank A enters the desorption stage, opens the 3rd valve 4, the 4th valve 5, the 8th valve 13, the 9th valve 14, the first valve A3, A4, uses N
2gas in exchange system, switch three-way valve 3 connects a, c end, and the gas displacing is sent into absorption front-end pipelines; When online oxygen conten analyser 10 detection system oxygen concentrations are less than 0.5%, switch three-way valve 3 connects a, b end, guarantee that desorption system pressure is after 4～10kpa, to close nitrogen gas supply the 3rd valve 4, the 4th valve 5, close the 8th valve 13, start circulation desorption blower fan 15, open the 6th valve 8, the 7th valve 9, open oil pump 7, heater 12 is started working, simultaneously open cold condenser 16, the air quantity that regulates shunt valve 17, system is carried out desorption condensation recovery.
High-concentration organic waste gas after desorb divides two parts, the part two-stage condensation equipment 16 of flowing through, and a part is through shunt valve 17, and then two parts gas mixes and gets back in circulating-heating loop, by circulating fan 15, sends the first absorbent charcoal adsorption tank A back to; The desorption gas of two-stage condensation equipment 16 of flowing through first carries out tentatively cooling through front end heat exchanger, can obtain partial organic substances cooling fluid, remaining gas enters further deep layer condensation in B grade condensing unit again, and cooling fluid and condensate recovery liquid enter purification system after intermediate storage tank 18.Condensed remainder gas is again sent back to by heater 12 desorption that circulates in the first absorbent charcoal adsorption tank A after desorption gas through shunt valve 17 mixes.When reaching, set after desorption time, by PLC control system, close heater 12, close the 9th valve 14, open the 8th valve 13, open cold condenser 11, the first absorbent charcoal adsorption tank A carry out cooling processing simultaneously.Partial condensation air quantity is respectively 1:1 with the ratio of shunt valve air quantity, and system desorption temperature is set 90 ℃.
The variation of the oxygen content in online oxygen conten analyser 10 real-time monitoring systems, and control processing by PLC system, in desorption system, give the alarm during oxygen content > 2%, heater 12 stops heating, close circulating fan 15, open the 3rd valve 4, the 4th valve 5, the first valve A2, carry out nitrogen replacement in system, when oxygen content < 0.5%, reopen desorption manipulation.
Four, when the first absorbent charcoal adsorption tank A charcoal layer temperature reaches the following temperature of VOCs boiling point, open anti-purging system: close condenser 11, close the 8th valve 13, open the 5th valve 6, the 9th valve 14, connecting tee valve a, c end, it is VOCs boiling temperature that heater 12(sets heter temperature), system is carried out blowback and is swept.The gas purging out through triple valve a, c end send back to absorption front-end preprocessor system enter table cold filter 1 carry out pretreatment.Blowback flyback time is 20% of desorption time, and anti-purge air quantity is desorption air quantity.After finishing, purging closes heater 12 and the 9th valve 14, open cold condenser 11 and the 8th valve 13, and gas is sent into the first absorbent charcoal adsorption tank A after by condenser 11 to reduce charcoal layer temperature, so that next recycles.
Five, step 1, two, three, four selfs are moved and are looped, and two adsorption tanks replace adsorption and desorption, cooling.
Six, technological process of the present invention is by PLC control program system by completing the analyzing and processing of the detection data such as the pressure of system, temperature, oxygen content, and whole process is controlled automatically.
In the present invention, show cold filter and belong to front-end preprocessor system, it is mainly used in most suspended substances and granule foreign in filtration treatment organic exhaust gas, regulates EGT, the service life that is conducive to improve the absorption property of active carbon and extends active carbon; The variation of oxygen content concentration in oxygen conten analyser on-line real time monitoring system, guarantees the safe operation of system; Circulation desorption blower fan, is the mobile power of gas circulation in desorption system, can allow nitrogen circulation use, and saves the consumption of nitrogen; Shunt valve, makes the hot gas after part desorption directly from bypass, by circulating fan, send adsorption tanks back to without condensation, to reduce the heat exchange area of condenser, realizes recycling of heat, reduces energy consumption.
The present invention adopts partial condensation to reclaim and reverse purging process, not only effectively solved prior art problem, greatly simplified technique, reduced production cost, and overcome the limitation that in desorption removal process in the past, energy consumption is high, heat transmission equipment has high input, the organic matter quality purer feature that has kept hot gas desorption to reclaim; In addition, technological process of the present invention by the detection analyzing and processing to data such as the pressure of system, temperature, oxygen contents, realizes whole-process automatic control by PLC control program system.
Although more than described the specific embodiment of the present invention; but being familiar with those skilled in the art is to be understood that; our described specific embodiment is illustrative; rather than for the restriction to scope of the present invention; those of ordinary skill in the art are in equivalent modification and the variation done according to spirit of the present invention, all should be encompassed in the scope that claim of the present invention protects.
Claims (6)
1. a charcoal absorption, N
2the technique of desorption recycling organic exhaust gas, is characterized in that: described processing step is as follows:
Step 10, organic exhaust gas enter the cold filter of table by main air blower and carry out pretreatment, and organic exhaust gas after pretreatment is sent into the first absorbent charcoal adsorption tank again and adsorbed;
Step 20, when absorption arrives a default breakthrough point, close and open corresponding valve, make the first absorbent charcoal adsorption tank enter the desorption system stage, the second absorbent charcoal adsorption tank enters the adsorption system stage;
N in step 30, use storage nitrogen tank
2replace the gas in the first absorbent charcoal adsorption tank, and the gas displacing is sent back in the cold filter of table, by the second absorbent charcoal adsorption tank, carry out adsorption treatment; When online oxygen analyser detects desorption system oxygen content and is less than 0.5%, control desorption system pressure and after 4～10KPa, close N
2supply with, add N in thermal desorption system pipeline
2the ON cycle blower fan desorption that circulates, desorption organic exhaust gas out divides two parts, the part two-stage condensation equipment of flowing through, a part is through shunt valve, then two parts gas mixes, and by circulating fan, is sent in heater and is carried out heat treated, then reenters in the first absorbent charcoal adsorption tank and proceeds desorption; After the high-concentration organic waste gas condensation of flowing through after the desorption of two-stage condensation equipment, enter purification system;
After step 40, desorption finish, charcoal layer temperature in the first absorbent charcoal adsorption tank drops to the boiling temperature of VOCs gas when following, close and open corresponding valve, extraction fresh air carries out blowback to be swept, and heats this fresh air to the boiling temperature of VOCs gas simultaneously; The gas purging out enters in the cold filter of table again, by the second absorbent charcoal adsorption tank, carries out adsorption treatment;
Step 50, blowback are swept after end, and intrasystem gas is carried out to condensation cooling, finally by this condensed gas, the charcoal layer in the first absorbent charcoal adsorption tank are lowered the temperature, so that next recycles;
Described the first absorbent charcoal adsorption tank and the above step of the second absorbent charcoal adsorption tank cycle alternation.
2. the technique of a kind of charcoal absorption according to claim 1, N2 desorption recycling organic exhaust gas, it is characterized in that: in described step 30, the organic exhaust gas of desorption of two-stage condensation equipment of flowing through first carries out tentatively cooling through two-stage condensation front equipment end heat exchanger, can obtain partial organic substances cooling fluid, remaining gas enters further deep layer condensation in B grade condensing unit again, and cooling fluid and condensate recovery liquid enter purification system after intermediate storage tank; Condensed remainder gas is sent the desorption that circulates in the first absorbent charcoal adsorption tank again after heating by heater after desorption organic exhaust gas through shunt valve mixes.
3. the technique of a kind of charcoal absorption according to claim 1 and 2, N2 desorption recycling organic exhaust gas, it is characterized in that: in described step 30, partial condensation air quantity is respectively 1:1～1:12 with the ratio of bypass air quantity, 80～350 ℃ of desorption system Temperature Settings.
4. the technique of a kind of charcoal absorption according to claim 1, N2 desorption recycling organic exhaust gas, it is characterized in that: in described step 30, when line oxygen conten analyser detects in desorption system oxygen content > 2%, give the alarm, desorption system stops heating and circulation desorption, opens corresponding valve, again carries out nitrogen replacement in system, when oxygen content < 0.5%, reopen desorption manipulation.
5. the technique of a kind of charcoal absorption according to claim 1, N2 desorption recycling organic exhaust gas, is characterized in that: described blowback flyback time is desorption time 20%～30%; Described anti-purge air quantity equates with desorption air quantity.
6. the technique of a kind of charcoal absorption according to claim 1, N2 desorption recycling organic exhaust gas, is characterized in that: described technique is by PLC control program system whole-process automatic control.
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