CN109821342A - A kind of TREATMENT OF VOCs device and processing method - Google Patents
A kind of TREATMENT OF VOCs device and processing method Download PDFInfo
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- CN109821342A CN109821342A CN201910234562.5A CN201910234562A CN109821342A CN 109821342 A CN109821342 A CN 109821342A CN 201910234562 A CN201910234562 A CN 201910234562A CN 109821342 A CN109821342 A CN 109821342A
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- 239000012855 volatile organic compound Substances 0.000 title claims abstract description 23
- 238000003672 processing method Methods 0.000 title abstract description 3
- 238000010521 absorption reaction Methods 0.000 claims abstract description 44
- 239000006096 absorbing agent Substances 0.000 claims abstract description 37
- 239000007788 liquid Substances 0.000 claims abstract description 37
- 238000001179 sorption measurement Methods 0.000 claims abstract description 37
- 238000000034 method Methods 0.000 claims abstract description 11
- 239000000463 material Substances 0.000 claims abstract description 3
- 238000012856 packing Methods 0.000 claims abstract description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 21
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- 238000010792 warming Methods 0.000 claims description 13
- 238000010438 heat treatment Methods 0.000 claims description 11
- 238000000605 extraction Methods 0.000 claims description 6
- 239000005416 organic matter Substances 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 2
- 238000011084 recovery Methods 0.000 abstract description 7
- 238000004064 recycling Methods 0.000 abstract description 3
- 238000004140 cleaning Methods 0.000 abstract description 2
- 238000004134 energy conservation Methods 0.000 abstract 1
- 230000007613 environmental effect Effects 0.000 abstract 1
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 37
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 32
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 17
- 238000004519 manufacturing process Methods 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- DHMQDGOQFOQNFH-UHFFFAOYSA-N Glycine Chemical compound NCC(O)=O DHMQDGOQFOQNFH-UHFFFAOYSA-N 0.000 description 4
- 239000002250 absorbent Substances 0.000 description 4
- 230000002745 absorbent Effects 0.000 description 4
- 238000009835 boiling Methods 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000000945 filler Substances 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 239000004471 Glycine Substances 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 235000019441 ethanol Nutrition 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 208000031320 Teratogenesis Diseases 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 230000000711 cancerogenic effect Effects 0.000 description 1
- 231100000315 carcinogenic Toxicity 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 230000007794 irritation Effects 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a kind of TREATMENT OF VOCs device and processing methods.Adsorption tanks are connect through air-introduced machine with cyclone separator, and cyclone separator is connect with packed absorber；Packing material absorbing tower bottom is pumped through packed tower spray-absorption and is connect with level-one preheater；Level-one preheater is connect with tail gas first-stage condenser, and tail gas first-stage condenser is connect with second level preheater；Second level preheater is connect with rectifying column, and rectifier bottoms are connected to discharge tank.Specific steps are as follows: VOCs is delivered in packed absorber by air-introduced machine and carries out spray-absorption with absorbing liquid, the VOCs not absorbed carries out high tower emptying after the adsorption tower equipped with adsorption stuffing is absorbed, the absorbing liquid of absorption returns to absorption tower after rectifying column parses, the VOCs component distillated is for producing and using, VOCs recycling may be implemented in the method, and realizes tail gas VOCs cleaning discharge.This method equipment investment is small, energy conservation and environmental protection, is suitable for volatile organic compounds recovery technique.
Description
Technical field
The present invention relates to a kind of TREATMENT OF VOCs device, specially a kind of dress of volatile organic compounds recovery processing
It sets.
Background technique
Because most of volatile organic matters (VOCs) lead to city gray haze, atmospheric ozone layer pollution and photochemical fog
Important as precursors object, and have the characteristics that toxicity, irritation, teratogenesis and carcinogenic.Therefore country puts into effect relevant laws and regulations limit
The discharge of VOCs processed.Currently, administering VOCs technology mainly has condensing recovery, adsorption recovery and burning etc..Because of condensing recovery and suction
Attached recovery technology, condensed absorbent efficiency is lower, and the exhaust gas that absorption tower comes out is there is also problem not up to standard, and incineration technology
It easily causes the wasting of resources and burning insufficient easily causes secondary pollution.
Summary of the invention
For overcome the deficiencies in the prior art, the present invention provides volatile organic compounds recovery processing equipment and its recycling sides
Method, VOCs are delivered in packed absorber by air-introduced machine and carry out spray-absorption with absorbing liquid, and the VOCs not absorbed is by dress
High tower emptying is carried out after having the adsorption tower of adsorption stuffing to be absorbed, the absorbing liquid of absorption returns to absorption after rectifying column parses
Tower, for the VOCs component distillated for producing and using, which may be implemented VOCs recycling, and realize tail gas VOCs cleaning row
It puts.
The TREATMENT OF VOCs device, including adsorption tanks, air-introduced machine, cyclone separator, packed absorber, one
Grade condenser, packed tower spray-absorption pump, level-one preheater, secondary condenser, rectifying column produce pump, tail gas first-stage condenser,
Tail gas secondary condenser, rectifying column, tail gas receiving tank, second level preheater,
Adsorption tanks are connect through air-introduced machine with cyclone separator, and cyclone separator is connect with packed absorber；
Packing material absorbing tower bottom is pumped through packed tower spray-absorption and is connect with level-one preheater；
The packed absorber is stainless steel cloth packed tower or ceramic corrugated filler tower, volatility VOCs
Gas is alcohols such as methanol or ethyl alcohol, and absorbing liquid is water.
Level-one preheater is connect with tail gas first-stage condenser, and tail gas first-stage condenser is connect with second level preheater；
Second level preheater is connect with rectifying column, and rectifier bottoms are connected to discharge tank.
The packed tower spray-absorption pump is also connect with first-stage condenser, and first-stage condenser is connected to packed absorber；
The level-one preheater is also connect with packed absorber.
The second level preheater is connect through rectifying column extraction pump with secondary condenser, and secondary condenser connection is pre- with level-one
Hot device connection.
The tail gas first-stage condenser is also connect with tail gas secondary condenser, and tail gas secondary condenser and tail gas receive
Tank.
The absorption pot bottom is also connect with packed absorber.
On the basis of above-mentioned apparatus, the present invention also provides a kind of methods for handling volatile organic matter VOCs, including such as
Lower step:
(1) absorbing liquid is added into packed absorber, control absorbing tower liquid-level is 0.4-0.8m, opens absorption tower spray-absorption
Pump, a part of absorbing liquid cools down through first-stage condenser carries out self-loopa, and a part of pregnant solution is cold through level-one preheater, tail gas level-one
Rectifying column is removed in condenser, the heating of second level preheater；
A part of absorbing liquid described in the step (1) is cooled to 5-10 DEG C through first-stage condenser；A part of pregnant solution according to
It is secondary to remove rectifying column again after level-one preheater, tail gas first-stage condenser, second level preheater are warming up to 50-55 DEG C, while control is gone
Rectifying column flow is 2-4m3/h.The absorbing liquid includes water, benzene, toluene.
Make absorbent with benzene, absorb ether gas, using boiling point difference, ether rectifying is come out；
Make absorbent with toluene, absorb acetone gas, using boiling point difference, acetone rectifying is come out；
Make absorbent with water, absorb acetone gas, using boiling point difference, acetone rectifying is come out.
(2) open air-introduced machine take out volatility VOCs gas, gas respectively through packed absorber and cyclone separator processing after,
The adsorption tower equipped with adsorption stuffing is removed, direct high tower emptying after qualified；Adsorption tower one is opened one standby, and VOCs is enriched with full adsorption tower and needs
90-100 DEG C first is warming up to steam to be parsed, be then cooled to 20-40 DEG C in case using next time, entire resolving needs
Want 6-10 hours.
(3) pregnant solution is gone into rectifying column, control tower bottom and tower top temperature through heating, controls rectifying column liquid level, distillates
VOCs group lease making tail gas first-stage condenser, tail gas secondary condenser condense to tail gas receiving tank for producing and using, and raffinate removes filler
Absorption tower.Absorbing liquid (pregnant solution) is removed into rectifying column through heating, control column bottom temperature is 100-107 DEG C, 50-75 DEG C of tower top, is controlled
Rectifying column liquid level processed is 0.4-0.8m, and for the VOCs component distillated for producing and using, raffinate goes to absorption tower.
Absorbing liquid dosage is not increased newly using technical solution of the present invention, reduces the processing cost of absorbing liquid, absorbing liquid can weigh
It is multiple to use, reduce production cost；
Absorbing liquid is added into packed absorber, controls absorbing tower liquid-level, opens absorption tower spray-absorption and pumps, one
It partially absorbs liquid and carries out self-loopa through first-stage condenser cooling, a part of pregnant solution is cold through level-one preheater, tail gas level-one
Rectifying column is removed in condenser, the heating of second level preheater；
Because absorbing liquid absorb VOCs gas uptake be it is certain, it exists always in rectifying column and absorption tower
It absorbs and parses, total amount is constant to be reused.
Adsorbent regeneration effect is good, can reuse.Because adsorption tower one is opened one standby, VOCs is enriched with full adsorption tower and needs elder generation
90-100 DEG C is warming up to steam to be parsed, and is then cooled to 20-40 DEG C in case using next time, entire resolving needs 6-
10 hours.So adsorbent can be reused, regeneration effect is preferable.
Distillation system is closed cycle, VOC free s gas overflowing.In distillation system, because of VOCs gas phase pipe
Line is closed, no outlet and tonifying Qi pipeline through I and II condenser to tail gas receiving tank.
This method has the following advantages:
(1) automation degree of equipment is high, automatic control can control entirely, realize unmanned control.
(2) VOCs vent gas treatment effect is good, can reach national emission standard.
(3) package unit is mutually exchanged heat using rectifying column steam condensate (SC), need to only assist a small amount of cold energy, cold and hot energy sufficiently benefit
With reduction production cost.
(4) VOCs recycled can use production process, reduce production cost.
Detailed description of the invention
Fig. 1 is a kind of TREATMENT OF VOCs device, wherein 1. adsorption tanks, 2. air-introduced machines, and 3. cyclone separators, 4.
Packed absorber, 5. first-stage condensers, 6. packed tower spray-absorptions pump, 7. level-one preheaters, 8. secondary condensers, 9. rectifying columns
Extraction pump, 10. tail gas first-stage condensers, 11. tail gas secondary condensers, 12. rectifying columns, 13. tail gas receiving tanks, 14. second levels are pre-
Hot device.
Specific embodiment
Embodiment 1
A kind of TREATMENT OF VOCs device, including adsorption tanks 1, air-introduced machine 2, cyclone separator 3, packed absorber 4, level-one
Condenser 5, packed tower spray-absorption pump 6, level-one preheater 7, secondary condenser 8, rectifying column extraction pump 9, the condensation of tail gas level-one
Device 10, tail gas secondary condenser 11, rectifying column 12, tail gas receiving tank 13, second level preheater 14, adsorption tanks 1 are through air-introduced machine 2 and rotation
Wind separator 3 connects, and cyclone separator 3 is connect with packed absorber 4, and the filler in the packed absorber is high-efficiency activated
Charcoal or efficient molecular sieve；4 bottom of packed absorber is connect through packed tower spray-absorption pump 6 with level-one preheater 7；Level-one preheater
7 connect with tail gas first-stage condenser 10, and tail gas first-stage condenser 10 is connect with second level preheater 14；Second level preheater 14 and rectifying
Tower 12 connects, and 12 bottom of rectifying column is connected to discharge tank.
Packed tower spray-absorption pump 6 is also connect with first-stage condenser 5, and first-stage condenser 5 is connected to packed absorber 4；Institute
The level-one preheater 7 stated also is connect with packed absorber 4.Second level preheater 14 connects through rectifying column extraction pump 9 with secondary condenser 8
It connects, the connection of secondary condenser 8 is connect with level-one preheater 7.Tail gas first-stage condenser 10 is also connect with tail gas secondary condenser 11,
Tail gas secondary condenser 11 and tail gas receiving tank 13.1 bottom of adsorption tanks is also connect with packed absorber 4.
Embodiment 2
For extracting methanol used during glycine produces, water is added into packed absorber, control absorbing tower liquid-level is 0.6m,
Packed tower spray-absorption pump is opened, a part of water first-stage condenser is cooled to 10 DEG C of progress self-loopas, a part of water (pregnant solution)
50 DEG C successively are warming up to through level-one preheater, tail gas first-stage condenser, second level preheater and removes rectifying column, and rectifying column flow is removed in control
For 2m3/h.It opens air-introduced machine and takes out methanol gas, gas after packed absorber and cyclone separator processing, is gone equipped with work respectively
Property charcoal adsorption tower absorption after high tower empty；Adsorption tower one is opened one standby, and methanol gas is enriched with full adsorption tower and needs first to use steam
100 DEG C are warming up to be parsed, then with air cooling-down to 26 DEG C it is spare, entire resolving needs 6 hours.By water (enrichment
Liquid) through heating remove rectifying column, control column bottom temperature is 98 DEG C, and 60 DEG C of tower top, control rectifying column liquid level is 0.8m, the methanol distillated
For component for producing and using, raffinate is 2m with flow3/ h rectifying column extraction pump goes to absorption tower through condenser, level-one preheater.Through
Without methanol gas and rectifying column can recycle 95% methanol solution there are tail gas receiving tanks in line detection high tower vent gas.
Embodiment 3
For extracting methanol used during glycine produces, water is added into packed absorber, control absorbing tower liquid-level is 0.8m,
Open packed tower spray-absorption pump, a part of water first-stage condenser is cooled to 7 DEG C of progress self-loopas, a part of water (pregnant solution) according to
Secondary to be warming up to 55 DEG C through level-one preheater, tail gas first-stage condenser, second level preheater and remove rectifying column, control goes the rectifying column flow to be
3m3/h.It opens air-introduced machine and takes out methanol gas, gas after packed absorber and cyclone separator processing, is gone equipped with activity respectively
High tower empties after the adsorption tower absorption of charcoal；Adsorption tower one is opened one standby, and methanol gas is enriched with full adsorption tower and needs first with steam liter
Temperature is parsed to 100 DEG C, then with air cooling-down to 24 DEG C it is spare, entire resolving needs 8 hours.By water (pregnant solution)
Rectifying column is removed through heating, control column bottom temperature is 100 DEG C, and 62 DEG C of tower top, control rectifying column liquid level is 0.6m, the methanol group distillated
Divide for producing and using, raffinate is 3m with flow3/ h produces pump with rectifying column and goes to absorption tower through condenser, level-one preheater.Through
Without methanol gas and rectifying column can recycle 92% methanol solution there are tail gas receiving tanks in line detection high tower vent gas.
Embodiment 4
By taking extractant ether as an example, benzene is added into packed absorber, control absorbing tower liquid-level is 0.7m, opens packed tower spray
Absorption pump, a part of benzene are cooled to 10 DEG C of progress self-loopas through first-stage condenser, and a part of benzene (pregnant solution) is successively pre- through level-one
Hot device, tail gas first-stage condenser, second level preheater are warming up to 40 DEG C and remove rectifying column, and it is 3m that rectifying column flow is removed in control3/h.It opens
Air-introduced machine takes out ether gas, and gas after packed absorber and cyclone separator processing, removes the adsorption tower equipped with active carbon respectively
High tower empties after absorption；Adsorption tower one open it is one standby, ether gas be enriched with full adsorption tower need first with steam be warming up to 80 DEG C into
Row parsing, then with air cooling-down to 22 DEG C it is spare, entire resolving needs 6 hours.Benzene (pregnant solution) is gone into essence through heating
Tower is evaporated, control column bottom temperature is 82 DEG C, and 37 DEG C of tower top, control rectifying column liquid level is 0.8m, and the ether component distillated makes for production
With raffinate is 3m with flow3/ h produces pump with rectifying column and goes to absorption tower through condenser, level-one preheater.Through on-line checking high tower
Without ether gas and rectifying column can recycle 99% diethyl ether solution there are tail gas receiving tanks in vent gas.
Embodiment 5
By taking extractant acetone as an example, toluene is added into packed absorber, control absorbing tower liquid-level is 0.6m, opens packed tower spray
Absorption pump is drenched, a part of toluene first-stage condenser is cooled to 5 DEG C of progress self-loopas, and a part of toluene (pregnant solution) is successively through level-one
Preheater, tail gas first-stage condenser, second level preheater are warming up to 65 DEG C and remove rectifying column, and it is 3m that rectifying column flow is removed in control3/h.It opens
It opens air-introduced machine and takes out acetone gas, gas after packed absorber and cyclone separator processing, goes the absorption equipped with active carbon respectively
High tower empties after tower absorption；Adsorption tower one is opened one standby, and acetone gas is enriched with full adsorption tower needs and is first warming up to 100 DEG C with steam
Parsed, then with air cooling-down to 26 DEG C it is spare, entire resolving needs 6 hours.By toluene (pregnant solution) through heating up
Rectifying column is removed, control column bottom temperature is 115 DEG C, and 62 DEG C of tower top, control rectifying column liquid level is 0.7m, and the acetone component distillated is for life
It produces and uses, raffinate is 3m with flow3/ h produces pump with rectifying column and goes to absorption tower through condenser, level-one preheater.Through on-line checking
Without acetone gas and rectifying column can recycle 99% acetone soln there are tail gas receiving tanks in high tower vent gas.
Embodiment 6
By taking extractant acetone as an example, water is added into packed absorber, control absorbing tower liquid-level is 0.8m, opens packed tower spray
Absorption pump, a part of water first-stage condenser are cooled to 7 DEG C of progress self-loopas, and a part of water (pregnant solution) successively preheats through level-one
Device, tail gas first-stage condenser, second level preheater are warming up to 50 DEG C and remove rectifying column, and it is 3m that rectifying column flow is removed in control3/h.Unlatching is drawn
Blower takes out acetone gas, and gas after packed absorber and cyclone separator processing, goes the adsorption tower equipped with active carbon to inhale respectively
Attached high tower emptying；Adsorption tower one is opened one standby, and acetone gas, which is enriched with full adsorption tower needs and is first warming up to 100 DEG C with steam, to carry out
Parsing, then with air cooling-down to 24 DEG C it is spare, entire resolving needs 8 hours.Water (pregnant solution) is gone into rectifying through heating
Tower, control column bottom temperature are 102 DEG C, and 64 DEG C of tower top, control rectifying column liquid level is 0.8m, and the acetone component distillated makes for production
With raffinate is 3m with flow3/ h produces pump with rectifying column and goes to absorption tower through condenser, level-one preheater.Through on-line checking high tower
Without acetone gas and rectifying column can recycle 99% acetone soln there are tail gas receiving tanks in vent gas.
Claims (9)
1. a kind of TREATMENT OF VOCs device, including adsorption tanks (1), air-introduced machine (2), cyclone separator (3), packing material absorbing
Tower (4), first-stage condenser (5), packed tower spray-absorption pump (6), level-one preheater (7), secondary condenser (8), rectifying column are adopted
(9), tail gas first-stage condenser (10), tail gas secondary condenser (11), rectifying column (12), tail gas receiving tank (13), second level are pumped out
Preheater (14), which is characterized in that
Adsorption tanks (1) are connect through air-introduced machine (2) with cyclone separator (3), and cyclone separator (3) is connect with packed absorber (4)；
Packed absorber (4) bottom is connect through packed tower spray-absorption pump (6) with level-one preheater (7)；
Level-one preheater (7) is connect with tail gas first-stage condenser (10), tail gas first-stage condenser (10) and second level preheater (14)
Connection；
Second level preheater (14) is connect with rectifying column (12), and rectifying column (12) bottom is connected to discharge tank.
2. TREATMENT OF VOCs device according to claim 1, which is characterized in that packed tower spray-absorption pumps (6)
It is also connect with first-stage condenser (5), first-stage condenser (5) is connected to packed absorber (4)；The level-one preheater (7) is also
It is connect with packed absorber (4).
3. TREATMENT OF VOCs device according to claim 1, which is characterized in that second level preheater (14) is through rectifying
Tower extraction pump (9) is connect with secondary condenser (8), and secondary condenser (8) connection is connect with level-one preheater (7).
4. TREATMENT OF VOCs device according to claim 1, which is characterized in that tail gas first-stage condenser (10) is also
It is connect with tail gas secondary condenser (11), tail gas secondary condenser (11) and tail gas receiving tank (13).
5. TREATMENT OF VOCs device according to claim 1, which is characterized in that adsorption tanks (1) bottom also with fill out
Expect absorption tower (4) connection.
6. using the side of the described in any item TREATMENT OF VOCs device processing volatile organic matter VOCs of claim 1-5
Method, which comprises the steps of:
(1) absorbing liquid is added into packed absorber, controls absorbing tower liquid-level, opens absorption tower spray-absorption pump, a part is inhaled
It receives liquid and carries out self-loopa through first-stage condenser cooling, a part of pregnant solution is pre- through level-one preheater, tail gas first-stage condenser, second level
Rectifying column is removed in hot device heating；
(2) it opens air-introduced machine and takes out volatility VOCs gas, gas after packed absorber and cyclone separator processing, goes to fill respectively
There is the adsorption tower of adsorption stuffing, direct high tower emptying after qualified；
(3) pregnant solution is gone into rectifying column, control tower bottom and tower top temperature through heating, controls rectifying column liquid level, the VOCs group distillated
Lease making tail gas first-stage condenser, tail gas secondary condenser condense to tail gas receiving tank for producing and using, and raffinate removes packed absorber.
7. the method for processing volatile organic matter VOCs according to claim 6, which is characterized in that the absorbing liquid packet
Include water, benzene, any one in toluene.
8. the method for processing volatile organic matter VOCs according to claim 6, which is characterized in that described in step (1)
A part of absorbing liquid be cooled to 5-10 DEG C through first-stage condenser；A part of pregnant solution is successively through level-one preheater, tail gas level-one
Condenser, second level preheater remove rectifying column again after being warming up to 50-55 DEG C, while it is 2-4m that rectifying column flow is removed in control3/h。
9. the method for processing volatile organic matter VOCs according to claim 6, which is characterized in that tower bottom in step (3)
Temperature is 100-107 DEG C, 50-75 DEG C of tower top.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112892158A (en) * | 2021-01-18 | 2021-06-04 | 天津红科朴业科技有限公司 | Comprehensive treatment process for tail gas containing carbon dioxide and chlorine-containing organic matters |
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| CN112892158B (en) * | 2021-01-18 | 2022-04-15 | 天津红科朴业科技有限公司 | Comprehensive treatment process for tail gas containing carbon dioxide and chlorine-containing organic matters |
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