CN102489113B - Method for recovering organic solvent from organic waste gas - Google Patents
Method for recovering organic solvent from organic waste gas Download PDFInfo
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- CN102489113B CN102489113B CN 201110424881 CN201110424881A CN102489113B CN 102489113 B CN102489113 B CN 102489113B CN 201110424881 CN201110424881 CN 201110424881 CN 201110424881 A CN201110424881 A CN 201110424881A CN 102489113 B CN102489113 B CN 102489113B
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Abstract
The invention belongs to the technical field of treatment of organic waste gas, and relates to a method for recovering an organic solvent from organic waste gas. The method comprises the following steps of: adsorbing the organic solvent in the organic waste gas into active carbon, purifying, and discharge within controlling indexes of a national standard; when the active carbon is saturated by adsorbing, heating the residual organic waste gas in a pipeline, desorbing the organic solvent which is absorbed by the active carbon, and regenerating the active carbon; performing heat exchange on thedesorbed organic solvent gas, condensing into liquid, and recovering; and heating condensed waste gas, reentering the desorbed saturated active carbon again, circulating, and finishing one-time desorption. The method has the advantages of simple process flow, convenience for operating, saving in energy, reduction in production cost, lowering of the organic substance content of the waste gas to reach an environmentally-friendly emission standard, capability of recycling organic substances in the waste gas as resources, regeneration of active carbon, no emission of secondary pollutants, remarkable economic benefit and wide application field.
Description
Technical field
The invention belongs to the VOCs treatment technical field, relate to a kind of combined method by charcoal absorption-hot blast desorption-freezing recovery combination operation recovery organic solvent from organic water gas.
Background technology
Because organic solvent is of a great variety, use is extensive and consumption is huge, the not treated atmosphere that just enters of organic solvent gas, toxic side effect not only, also can produce acid fume mist, photochemical fog etc. in the troposphere of atmosphere, stratosphere at atmosphere consumes ozone, finally understands harm humans and vegeto-animal life security.Although and the organic solvent that reclaims and the mist of air can play detoxication through flaming combustion or flameless catalytic combustion, but still can produce a large amount of greenhouse gases carbon dioxide.Therefore hold back organic solvent gas by the way of liquid absorption, solid absorption and refrigerated condensation, be only the basic way that solves the solvent recovery problem.
But liquid absorption method can produce a large amount of waste water, and it is larger to process the waste water expense; The solid absorption method namely adopts charcoal absorption, although this method is that to adsorb at present the organic exhaust gas effect preferably most widely used general, but after charcoal absorption was saturated, active carbon had just lost the adsorption capacity to organic pollution, and this moment just or change active carbon, active carbon regenerated reuse, not only cost is high to change active carbon, and the labour intensity of changing is very large, but adopts traditional water vapour separating process regenerated carbon, also can cause waste water to produce, bring secondary pollution; Although it is high that the refrigerated condensation method reclaims solvent purity, recovering effect is little when organic solvent concentration is on the low side, and this method is used as the preliminary treatment of absorption process and absorption method often.
Summary of the invention
The object of the invention is the defective for prior art, and a kind of method that reclaims organic solvent from organic water gas is provided.The method makes the organic solvent resource, and regenerated carbon repeats to adsorb organic exhaust gas, thereby reaches environmental contamination reduction, reduces the wasting of resources, realizes the purpose of recycling economy.
For reaching above purpose, the technical solution adopted in the present invention is:
A kind of method that reclaims organic solvent from organic water gas comprises step:
(1) at first, the organic solvent in the organic exhaust gas is adsorbed in the active carbon qualified discharge after the organic exhaust gas after the adsorption treatment is purified;
(2) after charcoal absorption is saturated, with the organic exhaust gas that contains organic solvent remaining in the desorption exhaust piping by the saturated vapor indirect, the organic solvent that is adsorbed on the active carbon is carried out desorption, obtain high levels of organic solvents gas, make simultaneously regenerating active carbon;
(3) high levels of organic solvents gas and the condensed low-concentration organic exhaust gas that desorption gets off from the active carbon in the step (2) carried out heat exchange, the high levels of organic solvents condensation of gas to 20 that desorption is got off～40 ℃, alleviate the refrigerator load of step (4), simultaneously condensed low-concentration organic exhaust gas temperature is brought up to 60～80 ℃ from 0 ℃～-30 ℃, reduced the steam consumption of step (5);
(4) 20～40 ℃ of high levels of organic solvents that step (3) obtained pass through the freezing liquid condensation again, reclaim after being condensed into liquid solvent; Remaining low-concentration organic exhaust gas enters into step (3) exchange of reducing phlegm and internal heat again after the condensation;
(5) low-concentration organic exhaust gas that obtains in the step (4) is raised to 60～80 ℃ through the rear temperature of the exchange of reducing phlegm and internal heat in the step (3), enter the saturated active carbon of step (2) desorption through again being warmed up to 110 ℃～140 ℃ after the steam indirect again, so desorption is finished in circulation one time.
Described organic exhaust gas is the organic exhaust gas that produces in the printing industry printing ink, and it comprises in ethanol, ethyl acetate or the n-propyl acetate one or more.
The concentration range of organic solvent is 6～12g/m in the described high-concentration organic waste gas
3
The concentration range of organic solvent is 0～1g/m in the described low-concentration organic exhaust gas
3
The preferred Alveolate activated carbon capable of described active carbon.
Charcoal absorption temperature in the described step (1) is normal temperature.
Adsorption plant in the described step (1) is active carbon adsorber.
The heating-up temperature of described step (2) is 110 ℃～140 ℃, and the pressure of steam is 0.4～0.6MPa.
Low-concentration organic exhaust gas in the described step (3) is the gas that high levels of organic solvents gas obtains after through 0 ℃～-30 ℃ condensation.
The temperature of condensation recovery organic solvent is 0 ℃～-40 ℃ in the described step (4).
The temperature of the heating of waste gas is 110 ℃～140 ℃ in the described step (5).
Finish 6～8 hours circulation timei of desorption in the described step (5) one time.
In the step (2), with organic exhaust gas by indirect steam heating to 110 ℃～140 ℃, through desorption, the purpose of carrying out heat exchange with organic exhaust gas after freezing takes full advantage of the cold and hot energy exactly, because reclaiming organic solvent is to need low temperature, and carry out desorption organic solvent regenerated carbon again between 110 ℃～140 ℃ of high temperature, so in order not waste the energy each other, the two is carried out cold and hot exchange carry out the heat exchange first time, drop in temperature to 20～40 ℃, enter again freezing to 0 ℃～-40 ℃ recovery organic solvent liquid, and the organic exhaust gas after freezing by the heat exchange first time after its temperature be raised to 60～80 ℃, forming hot blast by steam indirect to 110 ℃～140 ℃ again continues deactivation charcoal absorber and carries out desorption work, closed circulation, cold energy, heat energy takes full advantage of.
Organic solvent condensate in the organic gas after freezing becomes the direct recycling of liquid, the organic solvent-free discharging, and non-secondary pollution produces.
Whole system is in airtight carrying out, and is safe and reliable without exhaust gas leakage, and good effect of heat exchange is not only energy-conservation but also reduce discharging.
Whole system so produce without waste water, does not have secondary pollution without adding assist medium, does not have wastewater treatment.
Owing to having adopted such scheme, the present invention has following characteristics:
1. flow process is simple, pretreatment process that need not be complicated;
2. active carbon long service life: by hot blast separating process regenerated carbon, prolonged the service life of active carbon, greatly reduced operating cost;
3. non-secondary pollution: by the more traditional water vapour separating process regenerated carbon of hot blast separating process regenerated carbon, produce without waste water, do not have secondary pollution, realized the cleaner production purpose;
4. through freezing, it is high that the high levels of organic solvents that desorption gets off reclaims purity, do not add other processing and namely can be recycled, and environmental contamination reduction reduces the wasting of resources, has realized the recycling economy purpose;
5. energy savings is passed through the exchange of hot and cold energy, and capacity usage ratio is high, and operating cost is low.
Description of drawings
Fig. 1 is process chart of the present invention.
The accompanying drawing mark:
1 active carbon adsorber, 2 absorption blower fans,
3 plate type heat exchangers, 4 evaporimeters,
5 desorption blower fans, 6 steam heaters,
7 mend air-cooler, 8 liquid collecting tanks.
The specific embodiment
The present invention is further illustrated below in conjunction with the accompanying drawing illustrated embodiment.
(1) concentrates organic exhaust gas (Q1), deliver to active carbon adsorber 1. by blower fan, carry out at normal temperatures adsorption cleaning, the organic pollution in the waste gas is by charcoal absorption, and 2. the organic gas (Q2) that reaches the cleaning gas standard is discharged in the atmosphere by the absorption blower fan and goes.
(2) after active carbon adsorber absorption was saturated, active carbon adsorber entered the hot blast desorption and regeneration stage.
In the desorption stage, utilize organic exhaust gas (we call it " cold wind ") remaining in the desorption exhaust piping through plate type heat exchanger 3. with evaporimeter 4., 5. be sent to steam heater 6. by the desorption blower fan, by from 0.4～0.6MPa saturated vapor indirect in the boiler room to temperature required 110 ℃～140 ℃ of desorption (we call it " hot blast "), hot blast enters heat activated charcoal in the active carbon adsorber, is adsorbed on organic pollution in the active carbon and spins off in the active carbon and form 6～12g/m
3High levels of organic solvents (Q3) makes regenerating active carbon simultaneously;
(3) with in the step (2) from the active carbon desorption high-temperature high concentration organic solvent (" hot blast ") out and condensed organic exhaust gas (Q5) (" cold wind ") carry out heat exchange at plate type heat exchanger in 3., " hot blast " temperature drops to (Q4) about 20～40 ℃, alleviate the refrigerator load of step (4), " cold wind " (Q5) then is warmed up to (Q6) about 60～80 ℃ by about 0 ℃～-40 ℃, has reduced the steam consumption of step (5);
(4) about 20～40 ℃ " hot blast " that step (3) is obtained (Q4) enters evaporimeter again and cools 0 ℃～-40 ℃ in 4., and at this moment, the organic solvent in the waste gas progressively condensation forms drop, enters liquid collecting tank 8. for subsequent use.And the organic concentration in the high levels of organic solvents also descends thereupon, then, this thigh " cold wind " (Q5) passes through heat exchanger again, carries out heat exchange with " hot blast ", the energy of fully recycling " hot blast ", simultaneously " hot blast " cooling also takes full advantage of the low-temperature receiver of " cold wind ".
(5) 6. " cold wind " that is warmed up to about 60～80 ℃ (Q6) 5. send into steam heater by the desorption blower fan again, be warming up to 110 ℃～140 ℃ (Q7) (hot blasts) by the steam indirect, enter in the active carbon adsorber 1. desorption and regeneration, finished whole circulation.Finish 6～8 hours circulation timei of desorption one time.
(6) during desorption by mending air-cooler operation 7., the temperature that control enters gas in the active carbon adsorber is no more than design temperature.
After desorption and regeneration was complete, the adsorption activity of active carbon adsorber was recovered, and reentered the absorption work of organic exhaust gas.
In actual moving process, 6. steam heater just the time needs full load to use the desorption startup stage with refrigeration system, arrive the temperature of setting when heating activated carbon after, owing to being provided with plate type heat exchanger, steam heater and refrigeration system all do not need the full load operation.So just can reach the energy and take full advantage of, reduce as far as possible the cost of active carbon desorption and regeneration.The open and close of steam heater and refrigeration system all are automatically to control according to auto temperature controlled system.
Charcoal absorption of the present invention-hot blast desorption-freezing recycling organic exhaust gas reclaims the organic solvent group technology, use checking in certain printing firm's VOCs treatment engineering, by the effect behind the actual motion, realized the spent organic solvent resource, the organic exhaust gas qualified discharge.
The above-mentioned description to embodiment is can understand and apply the invention for ease of those skilled in the art.The person skilled in the art obviously can easily make various modifications to these embodiment, and needn't pass through performing creative labour being applied in the General Principle of this explanation among other embodiment.Therefore, the invention is not restricted to the embodiment here, those skilled in the art are according to announcement of the present invention, and not breaking away from the improvement that category of the present invention makes and revise all should be within protection scope of the present invention.
Claims (10)
1. method that reclaims organic solvent from organic water gas is characterized in that: comprise following steps:
(1) at first the organic solvent in the organic exhaust gas is adsorbed in the active carbon qualified discharge after the organic exhaust gas of adsorption treatment is purified;
(2) after charcoal absorption is saturated, with the organic exhaust gas that contains organic solvent remaining in the desorption exhaust piping by the saturated vapor indirect, the organic solvent that is adsorbed on the active carbon is carried out desorption, obtain high levels of organic solvents gas, make simultaneously regenerating active carbon;
(3) high levels of organic solvents gas and the condensed low-concentration organic exhaust gas that desorption gets off from the active carbon in the step (2) carried out heat exchange, the high levels of organic solvents condensation of gas to 20 that desorption is got off～40 ℃, the temperature of this condensed low-concentration organic exhaust gas is brought up to 60～80 ℃ from 0 ℃～-30 ℃ simultaneously;
(4) 20～40 ℃ the high levels of organic solvents gas that step (3) is obtained passes through the freezing liquid condensation again, reclaims after being condensed into liquid solvent; Remaining low-concentration organic exhaust gas enters into step (3) exchange of reducing phlegm and internal heat again after the condensation;
(5) low-concentration organic exhaust gas that obtains in the step (4) is raised to 60～80 ℃ through the rear temperature of the exchange of reducing phlegm and internal heat in the step (3), enter the saturated active carbon of step (2) desorption through again being warmed up to 110 ℃～140 ℃ after the steam indirect again, so desorption is finished in circulation one time.
2. method according to claim 1, it is characterized in that: described organic exhaust gas is the organic exhaust gas that produces in the printing industry printing ink, it comprises in ethanol, ethyl acetate or the n-propyl acetate one or more.
3. method according to claim 1, it is characterized in that: the concentration range of organic solvent is 6～12g/m in the described high-concentration organic waste gas
3
Or the concentration range of organic solvent is 0～1g/m in the described low-concentration organic exhaust gas
3
4. method according to claim 1, it is characterized in that: described active carbon is Alveolate activated carbon capable.
5. method according to claim 1, it is characterized in that: the charcoal absorption temperature in the described step (1) is normal temperature.
6. method according to claim 1, it is characterized in that: the adsorption plant in the described step (1) is active carbon adsorber.
7. method according to claim 1, it is characterized in that: the heating-up temperature of described step (2) is 110 ℃～140 ℃, and the pressure of steam is 0.4～0.6MPa.
8. method according to claim 1 is characterized in that: the low-concentration organic exhaust gas in the described step (3) is the gas that high levels of organic solvents gas obtains after through 0 ℃～-30 ℃ condensation.
9. method according to claim 1 is characterized in that: to reclaim the temperature of organic solvent be 0 ℃～-40 ℃ in condensation in the described step (4).
10. method according to claim 1 is characterized in that: finishing desorption circulation timei in the described step (5) is 6～8 hours.
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201110424881 CN102489113B (en) | 2011-12-16 | 2011-12-16 | Method for recovering organic solvent from organic waste gas |
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201110424881 CN102489113B (en) | 2011-12-16 | 2011-12-16 | Method for recovering organic solvent from organic waste gas |
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| CN102489113A CN102489113A (en) | 2012-06-13 |
| CN102489113B true CN102489113B (en) | 2013-09-18 |
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Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103474122B (en) * | 2013-09-04 | 2016-02-10 | 清华大学 | The minimizing technology of tetrahydrofurfuryl alcohol in a kind of high temperature nuclear reactor fuel element factory effluent |
| CN103691254A (en) * | 2013-12-10 | 2014-04-02 | 武汉旭日华科技发展有限公司 | Method for reducing energy consumption of wet-process organic solvent recovering device |
| CN103752127B (en) * | 2014-01-03 | 2016-01-13 | 深圳劲嘉彩印集团股份有限公司 | The organic waste gas treatment equipment in intaglio printing workshop and processing method thereof |
| CN104815519A (en) * | 2015-04-09 | 2015-08-05 | 北京信诺海博石化科技发展有限公司 | Recovery technology for volatile oil gas in lightweight aromatic hydrocarbons filling process |
| CN104801146B (en) * | 2015-04-17 | 2017-02-01 | 李振华 | Device and process for recovering volatile organic gas |
| CN107906544B (en) * | 2018-01-03 | 2019-04-23 | 王汉 | A kind of circulating processing method of energy conservation and environmental protection of lacquering and stoving varnish drying stage exhaust gas |
| CN111185143A (en) * | 2020-02-25 | 2020-05-22 | 韶关市宏泰化工与环境工程研究所 | Waste activated carbon regeneration process and equipment |
| CN113813940A (en) * | 2021-09-29 | 2021-12-21 | 江苏科仕达实验室环保科技有限公司 | Saturated activated carbon activation regeneration treatment process and control method |
| CN116585848B (en) * | 2023-06-28 | 2024-02-27 | 广州华科环保工程有限公司 | Method for concentrated collection and resource regeneration after organic waste gas dispersion treatment in printing and dyeing industry |
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| JPS54110978A (en) * | 1978-02-21 | 1979-08-30 | Unitika Ltd | Adsorption treatment of exhaust gas |
| CN101024139A (en) * | 2006-12-31 | 2007-08-29 | 武汉旭日华科技发展有限公司 | Method and apparatus for absorbing and recovering volatile gas by active charcoal fiber |
| CN101284201A (en) * | 2008-06-02 | 2008-10-15 | 北京云辰天环保科技有限公司 | Organic waste gas treatment process without secondary pollution |
| CN202028320U (en) * | 2011-04-14 | 2011-11-09 | 深圳市山水乐环保科技有限公司 | Organic waste gas processing plant |
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Granted publication date: 20130918 Termination date: 20211216 |