CN105854513A - Treatment method for chlorinated paraffin waste gas - Google Patents

Treatment method for chlorinated paraffin waste gas Download PDF

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Publication number
CN105854513A
CN105854513A CN201610408374.6A CN201610408374A CN105854513A CN 105854513 A CN105854513 A CN 105854513A CN 201610408374 A CN201610408374 A CN 201610408374A CN 105854513 A CN105854513 A CN 105854513A
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waste gas
adsorbent
chlorinated hydrocarbon
hydrocarbon waste
desorption
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CN201610408374.6A
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Inventor
李翔
蒋云峰
毛兵
吴勇前
孔令鸟
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Zhejiang Qicai Eco Technology Co Ltd
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Zhejiang Qicai Eco Technology Co Ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/20—Organic adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/206—Organic halogen compounds
    • B01D2257/2064—Chlorine
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/702—Hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
    • B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)

Abstract

The invention discloses a treatment method for chlorinated paraffin waste gas. The treatment method comprises the steps that firstly, active carbon or resin serves as an adsorbent to adsorb hydrochloric ether waste gas; secondly, pulse water vapor at 100-120 DEG C is adopted for desorbing chlorinated paraffin organic matter on the adsorbent; thirdly, a desorption product is subjected to condensation recycling at minus 10 DEG C. The adsorbent generated after desorption is purged with hot air or hot nitrogen at 60-80 DEG C, and the recycled adsorbent is recycled for adsorbing chlorinated paraffin waste gas. The hydrochloric ether waste gas is subjected to filtering dust removal and condensation cooling, and then adsorbed with the adsorbent. According to the treatment method, it is proposed that low-temperature pulse water vapor is used for desorbing chlorinated paraffin, and the temperature is maintained for 30 min after introduction of water vapor is stopped; hydrochloric ether is hardly hydrolyzed, no corrosion to equipment is caused, and the desorbing recycling rate can reach 90% or above.

Description

A kind of processing method of chlorinated hydrocarbon waste gas
Technical field
The present invention relates to technical field of waste gas treatment, be specifically related to the process side of a kind of chlorinated hydrocarbon waste gas Method.
Background technology
Chlorinatedorganic, as a kind of important organic solvent and product intermediate, in fine chemistry industry, has The industries such as machine chemical industry, pesticide, printing and dyeing, medicine are widely used, in use, inevitably Evaporate, or disperse is in workshop air, or enter air, people and animals and plants health are caused danger Evil.Common chlorohydrocarbon waste gas mainly contains dichloromethane, chloroform, 1,2-dichloroethanes, chlorine One or more in propylene, benzyl chloride.
Conventional chlorinated hydrocarbon exhaust-gas resource technology mainly has absorption to reclaim and absorption and desorption method, but by Need to select suitable absorbent in absorption process, and desorption process is complex, in the application of historical facts or anecdotes border often By absorption method, the chlorohydrocarbon in waste gas is reclaimed, and absorption method accounts in all waste gases Treatment process Ratio reaches 27%.Chlorohydrocarbon reaches saturated after absorption, must experience the process that desorption reclaims, often Desorption means have hot-air desorption, hot nitrogen desorption, transformation desorption, steam desorption etc., but There is the potential safety hazard reaching the quick-fried limit of Organic substance in hot-air desorption, and hot nitrogen desorption and transformation desorption are deposited In the problem of high cost, steam desorption method due to steam heat content height and is relatively easy to get, economy, Safety is good, is the most most widely used recovery process, is widely used in being desorbed boiling point relatively low Low-molecular-weight hydrocarbon and aromatic series Organic substance.
But during steam desorption chlorohydrocarbon, temperature often reaches more than 140 DEG C, suffers from the drawback that perishable System equipment is high to equipment and materials performance requirement；Under high temperature, chlorohydrocarbon easily hydrolyzes, and product purity is not High；Desorption rate is only more than 80%.
Summary of the invention
The invention provides the processing method of a kind of chlorinated hydrocarbon waste gas, in processing procedure, chlorohydrocarbon Do not hydrolyze, it is possible to effectively recycle the chlorohydrocarbon in waste gas.
A kind of processing method of chlorinated hydrocarbon waste gas, including:
Step 1, with activated carbon or resin as adsorbent, adsorbs chlorinated hydrocarbon waste gas；
Step 2, uses 100～120 DEG C of pulsating water steams to take off the chlorinated hydrocarbon waste gas on adsorbent Attached；
Step 3, desorption product carries out condensation below-10 DEG C and reclaims.
The present invention is applicable to fine chemistry industry, petroleum refining, medicine, packages printing, pesticide, printing and dyeing etc. The organic exhaust gas containing chlorohydrocarbon that composition that industry is discharged in a organized way is more single, especially chlorohydrocarbon Concentration is 1000～60000mg/m3Chlorinated hydrocarbon waste gas.Additionally, the boiling of application claims chlorohydrocarbon Point the lowest (being usually no more than 150 DEG C), saturated vapor pressure is big, because high boiling point has as far as possible Machine thing desorption cycles is long, and easily equipment is caused corrosion, produces a large amount of waste water, cause two during separation Secondary pollution, adsorbent is not easy to be dried after desorption.Dichloromethane, 1,2-dichloroethanes, three chloromethanes Alkane, chloropropene etc. all can use the present invention to provide compared with low boiling and higher volatile chlorohydrocarbon waste gas Processing method.
In prior art, in the processing procedure of chlorinated hydrocarbon waste gas, chlorohydrocarbon can hydrolyze, no Can be recovered well, the processing method using the present invention to provide, be not susceptible to the hydrolysis of chlorohydrocarbon, Can be to the effective recycling in addition of the chlorohydrocarbon in chlorinated hydrocarbon waste gas.
The resource technology of chlorinated hydrocarbon waste gas, its technique is primarily directed to chlorinated hydrocarbon organic exhaust gas and sets Meter, is also applicable to other kinds of organic exhaust gas, and the present invention is different from existing steam and adds thermal desorption, But use low temperature pulse steam+thermal desorption to be desorbed by the chlorohydrocarbon adsorbed on the sorbent, should Technology solves chlorohydrocarbon high-temperature steam desorption facile hydrolysis and the corrosion-prone problem of equipment, and owing to steaming Stripping temperature is relatively low, relatively low to the pressure performance requirement of device, and security performance is high simultaneously.
In step 2, pulsating water steam, i.e. steam contact with adsorbent in a pulsed fashion, utilize water The pressure of steam itself carries out in-depth desorption to Organic substance.
As preferably, the adsorbent after desorption uses 60～80 DEG C of hot-airs or hot nitrogen purging, reclaims Adsorbent be recycled and reused for absorb chlorinated hydrocarbon waste gas.
Adsorbent after desorption remains large quantity of moisture, after needing to remove moisture, can adsorb Processing, the present invention uses hot-air or hot nitrogen to purge adsorbent, and dried adsorbent can Proceed the absorption of step 1.
Absorption in step 1 is carried out under room temperature (the most not taking heating or cooling means), uses two Individual adsorption tower realizes the processing method that the present invention provides, and two adsorption towers are respectively adsorption tower A and absorption Tower B, when adsorption tower A carries out the absorption in step 1, adsorption tower B carries out the desorption in step 2, desorption Adsorbent reuse after completing, in like manner, when adsorption tower B carries out the absorption in step 1, adsorption tower A is carried out Desorption in step 2, circulates successively.
Use double tower adsorbent equipment, B tower desorption during the absorption of A tower, it is ensured that device is transported for 24 hours continuously OK, the dual purpose of chlorohydrocarbon resource and energy-conserving and environment-protective has been reached.
In order to ensure process effect, it is preferable that chlorinated hydrocarbon waste gas is carried out successively dust removal by filtration and After condensation cooling, adsorbent is utilized to adsorb.
Dust removal by filtration is to remove the particulate matter in chlorinated hydrocarbon waste gas, prevents the hole quilt of adsorbent Block and cause losing efficacy.Condensation cooling is to ensure that waste gas is with the temperature of no more than room temperature and adsorbent Contact, it is ensured that the effect of absorption.
As preferably, before utilizing adsorbent to adsorb, use calcium chloride that chlorinated hydrocarbon waste gas is entered Row is dried.In dried chlorinated hydrocarbon waste gas, moisture is few, after reducing the interference of moisture, and absorption Agent can more effectively absorb chlorinated hydrocarbon material.
Activated carbon in step 1 (ature of coal or wooden) can use graininess, it would however also be possible to employ fine Dimension shape, the parameter index of the granular activated carbon preferably employed in the application is, diameter≤4mm, CTC value 60～80, iodine number about 1000, moisture is less than or equal to 5%, and ash is less than or equal to 12%, Grain intensity is more than or equal to 85, and the amount of activated carbon of 4mm～9mm particle diameter (number average bead diameter) accounts for 70% Above.The NACF preferably employed is, specific surface area is more than 1000m2/g.The tree preferably employed Fat is, the moisture content macroporous adsorbent resin less than 5%.
In order to improve the absorbability of adsorbent, it is preferable that adsorbent is at peroxidating or modified with reduction After reason, carry out the absorption of chlorinated hydrocarbon waste gas.After modification, the surface acidity of adsorbent or The content of basic group increases, the polarity on surface or nonpolar enhancing, correspondingly, to polar substances or The absorbability of apolar substance also can strengthen.
As preferably, use HNO3、HClO、H2SO4、Cl2、H2O2In at least one to suction Attached dose carries out oxidation modification process.
During process, adsorbent is immersed in HNO3、HClO、H2SO4、Cl2Aqueous solution, H2O2In, After 3h, it is dried to obtain modified adsorbent in 100 DEG C.
As preferably, use H2Or N2Adsorbent is carried out high temperature reduction process, or adsorbent is placed in Nitric acid carries out impregnation process.
In order to ensure that the absorption property of adsorbent gives full play to, the chlorinated hydrocarbon that every gram of activated carbon is corresponding gives up Throughput is 150～400mL/min.
As preferably, in step 2, after stopping being passed through pulsating water steam, it is incubated at least at 100～120 DEG C 30min.In insulating process, volatility based on chlorohydrocarbon self, it is ensured that be desorbed completely.
In order to make desorption fully carry out, it is preferable that the consumption of pulsating water steam is in chlorinated hydrocarbon waste gas At least 5 times of content of organics.Further preferably, the consumption of steam has in being chlorinated hydrocarbon waste gas 5～10 times of machine thing content.
The present invention proposes to use low temperature pulse steam to be desorbed chlorohydrocarbon, stops being passed through steam Rear insulation 30min, chlorohydrocarbon hydrolyzes hardly, corrosion-free to equipment, and the desorption response rate is up to 90% Above.
Detailed description of the invention
Embodiment 1
Certain chlorohydrocarbon waste gas A, waste gas air quantity 5000m3/ h, chlorohydrocarbon level 50000～60000mg/m3。
(1) column coal mass active carbon room temperature absorption: in chlorohydrocarbon waste gas A, chlorohydrocarbon level is 48000mg/m3, flow 1200mL/min, activated carbon amount of fill is 5g, and activated carbon is at about 180min Left and right reaches to adsorb saturated, and saturated extent of adsorption is every gram of activated carbon adsorption 0.45g chlorohydrocarbon.
(2) 110 DEG C of low temperature pulse steam desorptions: use the low temperature pulse of 5 times of chlorohydrocarbon quality Steam desorption absorption chlorohydrocarbon on the activated carbon, the mixed gas after desorption is under the conditions of-10 DEG C Condensation,
In triplicate, desorption rate is all more than 92% for detachment assays.After condensation, solution layering, takes oil phase And aqueous phase, use gas chromatogram qualitative analysis, do not find chlorohydrocarbon hydrolysis phenomena.
(3) moist activated carbon is dried: the activated carbon after 80 DEG C of hot nitrogen purge step (2) desorptions, N2Flow is that (flow velocity is about 0.07m/s to 300mL/min, the time of staying about 18s, air speed 196h-1), Activated carbon loads and is 30g, and after about 4.5h, activated carbon moisture content is reduced to less than 10%.
Embodiment 2
Certain chlorohydrocarbon waste gas B, exhaust gas flow 1.5L/min, chlorohydrocarbon level is about 25000mg/m3。
(1) column coal mass active carbon room temperature absorption: activated carbon amount of fill is 5g, adsorbs after 15min Rate is less than 90%, and saturated extent of adsorption is every gram of activated carbon adsorption 0.18g chlorohydrocarbon.
(2) 120 DEG C of low temperature pulse steam desorptions: use the low temperature pulse of 6 times of Organic substance quality Steam desorption absorption chlorohydrocarbon on the activated carbon, after stopping being passed through steam, protects at 110 DEG C Temperature 30min, the mixed gas after desorption condenses under the conditions of-10 DEG C.
After condensation, solution layering, takes oil phase and aqueous phase, uses gas chromatogram qualitative analysis, and chlorohydrocarbon reclaims Rear percent hydrolysis is about 0.1%, is desorbed less than high-temperature vapor.
Embodiment 3
Certain chlorohydrocarbon waste gas C, exhaust gas flow 1200mL/min, chlorohydrocarbon level 10000mg/m3。
(1) column wood activated charcoal room temperature absorption: activated carbon amount of fill is 5g, and activated carbon is about About 180min reaches to adsorb saturated, and saturated extent of adsorption is every gram of activated carbon adsorption 0.33g chlorohydrocarbon.
(2) 120 DEG C of low temperature pulse steam desorptions: use the low temperature pulse of 5 times of Organic substance quality Steam desorption absorption chloroform on the activated carbon, after stopping being passed through steam, at 120 DEG C Insulation 30min.Mixed gas after desorption condenses under the conditions of-10 DEG C.
Desorption rate is more than 92%, and after condensation, solution layering, takes oil phase and aqueous phase, fixed by gas chromatogram Property analyze, do not find chlorohydrocarbon hydrolysis phenomena.
Embodiment 4
Certain chlorohydrocarbon waste gas D, exhaust gas flow 1000mL/min, chlorohydrocarbon level 300mg/m3。
(1) macroporous adsorbent resin room temperature absorption: absorbent filling amount is 8g, and adsorbent is at about 320min Left and right reaches to adsorb saturated, and saturated extent of adsorption is every gram of adsorbent 0.35g chlorohydrocarbon.
(2) 100 DEG C of low temperature pulse steam desorptions: use the low temperature pulse of 6 times of Organic substance quality Steam desorption absorption chlorohydrocarbon on resin, after stopping being passed through steam, is incubated at 100 DEG C 30min.Mixed gas after desorption condenses under the conditions of-10 DEG C.
Desorption rate is about 90%, and after condensation, solution layering, takes oil phase and aqueous phase, fixed by gas chromatogram Property analyze, chlorohydrocarbon percent hydrolysis≤0.1%, far below high-temperature vapor be desorbed.
Embodiment 5
Certain chlorohydrocarbon waste gas A, waste gas air quantity 5000m3/ h, chlorohydrocarbon level 50000～60000mg/m3。
(1) column coal mass active carbon room temperature absorption: in chlorohydrocarbon waste gas A, chlorohydrocarbon level is 48000mg/m3, flow 1000mL/min, activated carbon amount of fill is 5g, and activated carbon is at about 120min Left and right reaches to adsorb saturated, and saturated extent of adsorption is every gram of activated carbon adsorption 0.41g chlorohydrocarbon.
(2) 100 DEG C of low temperature pulse steam desorptions: use the low temperature pulse of 3 times of chlorohydrocarbon quality Steam desorption absorption chlorohydrocarbon on the activated carbon, the mixed gas after desorption is under the conditions of-10 DEG C Condensation,
In triplicate, desorption rate is all more than 90% for detachment assays.After condensation, solution layering, takes oil phase And aqueous phase, use gas chromatogram qualitative analysis, do not find chlorohydrocarbon hydrolysis phenomena.
(3) moist activated carbon is dried: the activated carbon after 80 DEG C of hot nitrogen purge step (2) desorptions, N2Flow is that (flow velocity is about 0.07m/s to 300mL/min, the time of staying about 18s, air speed 196h-1), Activated carbon loads and is 30g, and after about 4.5h, activated carbon moisture content is reduced to less than 10%.
Embodiment 6
Certain chlorohydrocarbon waste gas B, exhaust gas flow 1.5L/min, chlorohydrocarbon level is about 25000mg/m3。
(1) macroporous adsorbent resin room temperature absorption: absorbent filling amount is 5g, adsorption rate after 15min Less than 90%, saturated extent of adsorption is every gram of adsorbent 0.20g chlorohydrocarbon.
(2) 100 DEG C of low temperature pulse steam desorptions: use the low temperature pulse of 4 times of Organic substance quality Steam desorption absorption chlorohydrocarbon on resin, after stopping being passed through steam, is incubated at 100 DEG C 60min, the mixed gas after desorption condenses under the conditions of-10 DEG C.
After condensation, solution layering, takes oil phase and aqueous phase, uses gas chromatogram qualitative analysis, and chlorohydrocarbon reclaims Rear percent hydrolysis is about 0.1%, is desorbed less than high-temperature vapor.
Embodiment 7
Certain chlorohydrocarbon waste gas C, exhaust gas flow 1200mL/min, chlorohydrocarbon level 10000mg/m3。
(1) NACF room temperature absorption: NACF amount of fill is 5g, and NACF exists About about 180min reaches to adsorb saturated, and saturated extent of adsorption is every gram of activated carbon adsorption 0.28g chloro Hydrocarbon.
(2) 120 DEG C of low temperature pulse steam desorptions: use the low temperature pulse of 7 times of Organic substance quality Steam desorption absorption chloroform on NACF, after stopping being passed through steam, at 120 DEG C Lower insulation 30min.Mixed gas after desorption condenses under the conditions of 0 DEG C.
Desorption rate is more than 93%, and after condensation, solution layering, takes oil phase and aqueous phase, fixed by gas chromatogram Property analyze, do not find chlorohydrocarbon hydrolysis phenomena.
Embodiment 8
Certain chlorohydrocarbon waste gas D, exhaust gas flow 1000mL/min, chlorohydrocarbon level 300mg/m3。
(1) column coal mass active carbon room temperature absorption: activated carbon amount of fill is 8g, and activated carbon is about About 320min reaches to adsorb saturated, and saturated extent of adsorption is every gram of activated carbon adsorption 0.24g chlorohydrocarbon.
(2) 110 DEG C of low temperature pulse steam desorptions: use the low temperature pulse of 5 times of Organic substance quality Steam desorption absorption chlorohydrocarbon on the activated carbon, after stopping being passed through steam, protects at 110 DEG C Temperature 60min.Mixed gas after desorption condenses under the conditions of-5 DEG C.
Desorption rate is about 95%, and after condensation, solution layering, takes oil phase and aqueous phase, fixed by gas chromatogram Property analyze, chlorohydrocarbon percent hydrolysis≤0.1%, far below high-temperature vapor be desorbed.
In each embodiment, activated carbon diameter≤4mm, CTC value (i.e. the adsorption rate to carbon tetrachloride) 60～80, iodine number about 1000, moisture is less than or equal to 5%, and ash is less than or equal to 12%, and granule is strong Degree is more than or equal to 85, and the amount of activated carbon of 4mm～9mm particle diameter (number average bead diameter) accounts for more than 70%； NACF specific surface area is more than 1000m2/g；Macroporous adsorbent resin moisture content is less than 5%.
Comparative example 1
Use 150 DEG C, about 0.6MPa high-temperature vapor desorption absorption benzyl chloride on the activated carbon, water Steam continuously enters adsorption tanks, and quality of activated carbon is about 10g, desorption time about 7min, chlorine after desorption The percent hydrolysis changing benzyl is about about 4%, and the most about 3% is hydrolyzed to benzyl alcohol, and about 1% generates benzyl ether etc. Other material.
Use the method described in embodiment 1, change desorption temperature, and pulsating water steam and chlorohydrocarbon Mass ratio, the desorption rate result obtained is as shown in table 1.
Table 1
From the mass ratio of table 1, desorption temperature and steam and chlorohydrocarbon, desorption rate all had shadow Ringing, under low temperature, desorption rate reduces, after the mass ratio of steam and chlorohydrocarbon increases to certain value, de- Attached rate is not further added by.

Claims (10)

1. the processing method of a chlorinated hydrocarbon waste gas, it is characterised in that including:
Step 1, with activated carbon or resin as adsorbent, adsorbs chlorinated hydrocarbon waste gas；
Step 2, uses 100～120 DEG C of pulsating water steams to take off the chlorinated hydrocarbon waste gas on adsorbent Attached；
Step 3, desorption product carries out condensation below-10 DEG C and reclaims.
2. the processing method of chlorinated hydrocarbon waste gas as claimed in claim 1, it is characterised in that desorption After adsorbent use 60～80 DEG C of hot-airs or hot nitrogen purging, the adsorbent of recovery be recycled and reused for inhale Receive chlorinated hydrocarbon waste gas.
3. the processing method of chlorinated hydrocarbon waste gas as claimed in claim 1, it is characterised in that to chlorine After carrying out dust removal by filtration and condensation cooling successively for hydro carbons waste gas, adsorbent is utilized to adsorb.
4. the processing method of chlorinated hydrocarbon waste gas as claimed in claim 1, it is characterised in that utilize Before adsorbent adsorbs, use calcium chloride that chlorinated hydrocarbon waste gas is dried.
5. the processing method of chlorinated hydrocarbon waste gas as claimed in claim 1, it is characterised in that absorption Agent, after peroxidating or modified with reduction process, carries out the absorption of chlorinated hydrocarbon waste gas.
6. the processing method of chlorinated hydrocarbon waste gas as claimed in claim 5, it is characterised in that use HNO3、HClO、H2SO4、Cl2、H2O2In at least one adsorbent is carried out at oxidation modification Reason.
7. the processing method of chlorinated hydrocarbon waste gas as claimed in claim 5, it is characterised in that use H2Or N2Adsorbent is carried out high temperature reduction process, or adsorbent is placed in nitric acid carries out at dipping Reason.
8. the processing method of chlorinated hydrocarbon waste gas as claimed in claim 1, it is characterised in that step In 2, after stopping being passed through pulsating water steam, it is incubated at least 30min at 100～120 DEG C.
9. the processing method of chlorinated hydrocarbon waste gas as claimed in claim 1, it is characterised in that pulse The consumption of steam is in chlorinated hydrocarbon waste gas at least 5 times of content of organics.
10. the processing method of chlorinated hydrocarbon waste gas as claimed in claim 1, it is characterised in that every Gram chlorinated hydrocarbon exhaust gas flow that adsorbent is corresponding is 150～400mL/min.
CN201610408374.6A 2016-06-08 2016-06-08 Treatment method for chlorinated paraffin waste gas Pending CN105854513A (en)

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CN106540508A (en) * 2016-12-27 2017-03-29 上海新阳半导体材料股份有限公司 Reclaim the device and method of volatility organic chloride gas
CN110267729A (en) * 2016-12-21 2019-09-20 Isca管理有限公司 Greenhouse gases and heavy metal are removed from discharge stream
CN110981732A (en) * 2020-01-03 2020-04-10 凯瑞环保科技股份有限公司 Refining device and method for by-product dimethyl carbonate in process of preparing ethylene glycol from coal
CN110975851A (en) * 2019-12-26 2020-04-10 江苏南大环保科技有限公司 Resin desorption regeneration method for adsorbing organic matters
CN112110447A (en) * 2020-09-23 2020-12-22 浙江工业职业技术学院 Preparation method of yellow wine vinasse-based activated carbon

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110267729A (en) * 2016-12-21 2019-09-20 Isca管理有限公司 Greenhouse gases and heavy metal are removed from discharge stream
CN106540508A (en) * 2016-12-27 2017-03-29 上海新阳半导体材料股份有限公司 Reclaim the device and method of volatility organic chloride gas
CN110975851A (en) * 2019-12-26 2020-04-10 江苏南大环保科技有限公司 Resin desorption regeneration method for adsorbing organic matters
CN110975851B (en) * 2019-12-26 2022-06-03 江苏南大环保科技有限公司 Resin desorption regeneration method for adsorbing organic matters
CN110981732A (en) * 2020-01-03 2020-04-10 凯瑞环保科技股份有限公司 Refining device and method for by-product dimethyl carbonate in process of preparing ethylene glycol from coal
CN112110447A (en) * 2020-09-23 2020-12-22 浙江工业职业技术学院 Preparation method of yellow wine vinasse-based activated carbon

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Application publication date: 20160817