CN109432955A - A kind of processing method containing water-insoluble VOCs tail gas - Google Patents
A kind of processing method containing water-insoluble VOCs tail gas Download PDFInfo
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- CN109432955A CN109432955A CN201811612729.9A CN201811612729A CN109432955A CN 109432955 A CN109432955 A CN 109432955A CN 201811612729 A CN201811612729 A CN 201811612729A CN 109432955 A CN109432955 A CN 109432955A
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- tail gas
- tower
- solvent
- water
- absorber
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- 239000012855 volatile organic compound Substances 0.000 title claims abstract description 67
- 238000003672 processing method Methods 0.000 title claims abstract description 14
- 239000002904 solvent Substances 0.000 claims abstract description 206
- 239000006096 absorbing agent Substances 0.000 claims abstract description 137
- 238000011084 recovery Methods 0.000 claims abstract description 79
- 238000010521 absorption reaction Methods 0.000 claims abstract description 69
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 64
- 238000000605 extraction Methods 0.000 claims abstract description 58
- 230000008929 regeneration Effects 0.000 claims abstract description 53
- 238000011069 regeneration method Methods 0.000 claims abstract description 53
- 239000002250 absorbent Substances 0.000 claims abstract description 35
- 230000002745 absorbent Effects 0.000 claims abstract description 35
- 239000008213 purified water Substances 0.000 claims abstract description 16
- 238000009833 condensation Methods 0.000 claims abstract description 12
- 230000005494 condensation Effects 0.000 claims abstract description 12
- 238000004064 recycling Methods 0.000 claims abstract description 11
- 239000002351 wastewater Substances 0.000 claims abstract description 10
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 claims description 19
- 239000000203 mixture Substances 0.000 claims description 11
- 239000002994 raw material Substances 0.000 claims description 5
- 150000008282 halocarbons Chemical class 0.000 claims description 4
- 238000002955 isolation Methods 0.000 claims description 4
- 239000007788 liquid Substances 0.000 claims description 4
- 239000005416 organic matter Substances 0.000 claims description 4
- 239000003960 organic solvent Substances 0.000 claims description 2
- 238000009834 vaporization Methods 0.000 claims description 2
- 230000008016 vaporization Effects 0.000 claims description 2
- 239000000126 substance Substances 0.000 abstract description 5
- 230000009102 absorption Effects 0.000 description 43
- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 description 17
- 238000000034 method Methods 0.000 description 17
- 230000008569 process Effects 0.000 description 13
- 238000001816 cooling Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- FXHOOIRPVKKKFG-UHFFFAOYSA-N N,N-Dimethylacetamide Chemical compound CN(C)C(C)=O FXHOOIRPVKKKFG-UHFFFAOYSA-N 0.000 description 4
- 238000009835 boiling Methods 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 229940113088 dimethylacetamide Drugs 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 239000002808 molecular sieve Substances 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 238000005457 optimization Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- OXHNLMTVIGZXSG-UHFFFAOYSA-N 1-Methylpyrrole Chemical compound CN1C=CC=C1 OXHNLMTVIGZXSG-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000012298 atmosphere Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical class ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 235000019387 fatty acid methyl ester Nutrition 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- -1 halogenated hydrocarbons methylene chloride Chemical class 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000005338 heat storage Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000004434 industrial solvent Substances 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- HNJBEVLQSNELDL-UHFFFAOYSA-N pyrrolidin-2-one Chemical compound O=C1CCCN1 HNJBEVLQSNELDL-UHFFFAOYSA-N 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
Classifications
-
- 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
- B01D53/14—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 absorption
- B01D53/1406—Multiple stage absorption
-
- 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
- B01D53/14—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 absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- 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
- B01D53/14—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 absorption
- B01D53/1487—Removing organic compounds
-
- 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
- B01D2257/708—Volatile organic compounds V.O.C.'s
-
- 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
- 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)
- Gas Separation By Absorption (AREA)
Abstract
The present invention provides a kind of processing method containing water-insoluble VOCs tail gas, and tail gas enters the solvent absorption section of tail gas absorber, water absorber portion is entered after the absorption of absorbent, from tail gas absorber top discharge after the absorption of purified water；Tail gas absorption tower bottom, which produces the rich solution containing water-insoluble VOCs and passes through, enters solvent regeneration tower with lean solution heat exchange, solvent reclamation top of tower produces water-insoluble VOCs gas phase, and the lean solution of solvent regeneration tower tower reactor extraction returns to the solvent absorption section of tail gas absorber after exchanging heat with rich solution as a part of absorbent；Tail gas absorber water absorber portion bottom produces waste water containing solvent and is sent into solvent recovery tower, the water vapour condensation rear portion of solvent recovery top of tower extraction returns to tail gas absorber water absorber portion as purified water, and solvent recovery tower tower reactor produces the solvent absorption section that recycling design returns to tail gas absorber as a part of absorbent.The present invention can effectively absorb the water-insoluble VOCs substance in tail gas, make tail gas qualified discharge.
Description
Technical field
The invention belongs to tail gas disposal technique fields, and in particular to the industries such as chemical industry, medicine, fiber, new material are containing non-aqueous
The process of dissolubility VOCs vent gas treatment is particularly suitable for the higher tail gas of concentration containing halogenated hydrocarbons.
Background technique
Most water-insoluble VOCs are that there are commonly solvents for the industries such as pharmacy, chemical industry, fiber, new material, and extensively
The organic synthesis raw material of application.It is more likely to produce and contains while using these water-insoluble VOCs as industrial chemicals or solvent
There is the tail gas of water-insoluble VOCs substance.Common water-insoluble VOCs has certain toxicity, has centainly to operator's health
It influences, and more severe to atmosphere environment impact.So the processing containing water-insoluble VOCs tail gas is imperative, and processing method
As key point.Such as containing halogen elements, conventional photochemical catalytic oxidation, heat storage type combustion (RTO) etc. in water-insoluble VOCs
Destruction technology is not applicable.The processing mode that industry mostly uses at present has: multi-stage condensing technology after humidification first condenses and adsorbs skill afterwards
Art, single-stage solvent absorption technology.
Multi-stage condensing technology after humidification, a large amount of water vapours are passed through in the tail gas of water-insoluble VOCs makes tail gas be humidified, so
The tail gas after humidification is subjected to multiple condensation afterwards, the mixed liquor of water-insoluble VOCs and water is layered in a reservoir then, is obtained
Water-insoluble VOCs and steam condensate.This technical limitation is in treatment process to be become after condensation using a large amount of steam and contained two
The waste water of chloromethanes is difficult to handle.And steam condensation needs larger power consumption, operating cost is higher.
Adsorption technology after first condensing, carries out cooling condensation to the tail gas containing water-insoluble VOCs first, then passes through molecule
Sieve water-insoluble VOCs in absorber absorption tail gas.Molecular sieve adsorber absorption efficiency is desorbed water-insoluble with steam after reducing
VOCs, and water-insoluble VOCs and steam condensate are isolated by multi-stage condensing.This technical limitation is in tail gas most of
For air, the condensation effect that cools down is limited.And parsing needs a large amount of steam, becomes the waste water containing methylene chloride after condensation and is difficult to locate
Reason.And molecular sieve absorber cost itself is higher, using molecular sieve is needed to change for a period of time, generates solid waste, equipment investment
And operating cost is higher.
Single-stage solvent absorption technology uses the high boiling solvents such as white oil, diesel oil, DOP, Fatty acid methyl ester as absorbent,
After being absorbed by single-stage absorption tower, then absorbent is parsed.Use white oil as absorbent, though white oil is mixture
Right boiling point is higher, but can contain a small amount of low-boiling point material, and the secondary pollution to tail gas is caused after volatilization；Using diesel oil, DOP, rouge
Fat acid formicester etc. is used as absorbent, itself has certain volatility, causes the secondary pollution to tail gas.And because absorbing when desorbing
Agent boiling point is very high, generally at 300 DEG C or more, needs very condition of high vacuum degree that could gasify, the methylene chloride dew point under this high vacuum
At -15 DEG C hereinafter, condensation is extremely difficult.
Summary of the invention
The purpose of the present invention is to provide a kind of processing methods containing water-insoluble VOCs tail gas, can effectively absorb tail
Water-insoluble VOCs substance in gas, makes tail gas qualified discharge, and have the advantage that and do not generate dangerous waste, water-insoluble
VOCs removal efficiency is high, and has the characteristics that low energy consumption, adaptable.
Processing method containing water-insoluble VOCs tail gas of the invention, includes the following steps:
Using the tail gas absorber with upper water absorber portion and lower part solvent absorption section, tail gas enters tail gas absorber
Solvent absorption section, tail gas enter water absorber portion after the absorption of solvent absorption section inner absorbent, and tail gas is by water absorber portion
From tail gas absorber top discharge after the absorption of purified water；
Rich solution of the tail gas absorption tower bottom extraction containing water-insoluble VOCs passes through the lean solution produced with solvent regeneration tower tower reactor and changes
Heat enters solvent regeneration tower, and solvent reclamation top of tower produces water-insoluble VOCs gas phase, the lean solution of solvent regeneration tower tower reactor extraction
A part after producing the rich solution heat exchange containing water-insoluble VOCs with tail gas absorption tower bottom as absorbent returns to tail gas and inhales
Receive the solvent absorption section of tower；
Tail gas absorber water absorber portion bottom produces waste water containing solvent and is sent into solvent recovery tower, the extraction of solvent recovery top of tower
Water vapour condensation rear portion as purified water return tail gas absorber water absorber portion, solvent recovery tower tower reactor extraction recycle it is molten
Agent returns to the solvent absorption section of tail gas absorber as a part of absorbent.
Wherein, tail gas enters from the solvent absorption section bottom of tail gas absorber, and absorbent is passed through from the top of solvent absorber portion,
Purified water is passed through from the top of water absorber portion；Rich solution containing water-insoluble VOCs enters solvent regeneration tower from middle part, waste water containing solvent
Enter solvent recovery tower from middle part；Pass through disconnected tower tray isolation between two absorber portions of tail gas absorber；Tail gas absorber, solvent
Liquid between regenerator, solvent recovery tower is pressurizeed by force (forcing) pump to be transported；The solvent regeneration tower and solvent recovery tower bottom
Further respectively have the reboiler for the vaporization that heats up again.
Wherein, the water-insoluble VOCs gas phase of solvent reclamation top of tower extraction after condensing, return as phegma by a part
Solvent regeneration tower is returned, a part is produced as water-insoluble organic matter product.
Wherein, the water vapour condensation rear portion of solvent recovery top of tower extraction returns to solvent recovery tower as phegma.
Wherein, solvent recovery tower tower reactor extraction recycling design is sent directly into tail gas absorber, or the lean solution with process heat exchange
Enter tail gas absorber through cooling again after cocurrent, or successively exchanged heat again after the lean solution cocurrent produced with solvent regeneration tower tower reactor,
Enter tail gas absorber after cooling.
Wherein, water-insoluble VOCs content is 100~30000mgm3 in raw material tail gas-1, the tail of qualified discharge after processing
Water-insoluble VOCs content is lower than 5~30mgm3 of discharge standard in gas-1；Absorbent and the volume containing water-insoluble VOCs tail gas
Than being 1:1000~1:10 for 1:1000~1:10, purified water and containing water-insoluble VOCs exhaust gas volumes ratio；Tail gas absorber tower
Top operating pressure is 100~500PaA, and tower top operation temperature is 0~50 DEG C, and tower reactor operating pressure is 102~502PaA, tower reactor
Operation temperature is 0~50 DEG C；Solvent reclamation column overhead operating pressure is 10~200KPaA, and operation temperature is 30~150 DEG C, tower
Kettle operating pressure is 12~202PaA, and tower reactor operation temperature is 120~195 DEG C；Solvent recovery tower top operating pressure be 10~
300KPaA, operation temperature are 80~190 DEG C, and tower reactor operating pressure is 12~302PaA, and tower reactor operation temperature is 120~195
℃；Absorbent is cooled to 5~50 DEG C before entering tail gas absorber.
Wherein, the absorbent is water-soluble good organic solvent, including dimethyl acetamide (DMAc), N- methyl pyrrole
Or mixtures thereof pure components solvents such as pyrrolidone (NMP), dimethyl sulfoxide (DMSO), one of solvent composition ratio are 5%
~95%；The preferably mixture of DMSO, DMAc, wherein the volume ratio of DMSO in the mixture is 65%-85%.
The present invention also provides the processing systems containing water-insoluble VOCs tail gas, including tail gas absorber, solvent regeneration tower
And solvent recovery tower；The tail gas absorber has upper water absorber portion and lower part solvent absorption section, and solvent absorption section is equipped with tail
Gas feed inlet；The tail gas absorption tower bottom extraction mouth is connected to through the heat exchanger channels all the way of heat exchanger with solvent regeneration tower, solvent
Regenerator tower reactor extraction another way heat exchanger channels of the mouth through heat exchanger are connected to the solvent absorption section of tail gas absorber；Tail gas absorption
Tower water absorber portion bottom extraction mouth be connected to solvent recovery tower, solvent recovery top of tower extraction mouth through solvent recovery tower condenser and
The connection of tail gas absorber water absorber portion, solvent recovery tower tower reactor extraction mouth are connected to the solvent absorption section of tail gas absorber.
Wherein, the tail gas feed inlet is set to the solvent absorption section bottom of tail gas absorber, and solvent regeneration tower tower reactor is adopted
The feed entrance point that outlet and solvent recovery tower tower reactor extraction mouth are connected to the solvent absorption section of tail gas absorber respectively is set to tail
At the top of the solvent absorption section of aspiration tower, solvent recovery top of tower produces the feed position that mouth is connected to tail gas absorber water absorber portion
It installs and is placed at the top of water absorber portion, the feed entrance point that tail gas absorption tower bottom extraction mouth is connected to solvent regeneration tower is set to solvent
In the middle part of regenerator, the feed entrance point that tail gas absorber water absorber portion bottom extraction mouth is connected to solvent recovery tower is set to solvent and returns
It receives in the middle part of tower；Pass through disconnected tower tray isolation between two absorber portions of tail gas absorber；Tail gas absorption tower bottom produces mouth, solvent again
Raw tower tower reactor extraction mouth, tail gas absorber water absorber portion bottom extraction mouth, solvent recovery tower tower reactor produce on the extraction pipeline of mouth
It is respectively arranged with force (forcing) pump；The solvent regeneration tower and solvent recovery tower bottom further respectively have reboiler.
Wherein, solvent reclamation top of tower extraction mouth is connected with solvent regeneration tower condenser, regenerator return tank in turn, regenerates
Tower return tank is equipped with the return flow line being connected to solvent reclamation top of tower；Solvent recovery top of tower extraction mouth is connected with recycling in turn
Tower condenser, solvent recovery tower return tank, solvent recovery tower return tank are equipped with the return flow line being connected to solvent recovery top of tower,
Solvent recovery tower return tank, which is additionally provided with, is connected to solvent recovery tower tower reactor extraction mouth with the solvent absorption section of tail gas absorber
Channel.
Wherein, solvent recovery tower tower reactor extraction mouth is directly connected to the solvent absorption section of tail gas absorber, or is changed with passing through
It is connected to again with the solvent absorption section of tail gas absorber after pipeline cocurrent after hot device heat exchange, or produces mouth with solvent regeneration tower tower reactor
Extraction pipeline cocurrent after be then connected to the solvent absorption section of tail gas absorber using heat exchanger；Solvent regeneration tower tower reactor is adopted
The feed pipe for the feed entrance point that outlet and solvent recovery tower tower reactor extraction mouth are connected to the solvent absorption section of tail gas absorber respectively
The first cooler is additionally provided on road；The feed entrance point that solvent recovery top of tower extraction mouth is connected to tail gas absorber water absorber portion
The second cooler is additionally provided on feed pipe.
Processing method and system of the present invention containing water-insoluble VOCs tail gas have the advantage that is inhaled using single column two-stage
It receives, effectively improves absorption efficiency and save equipment investment；It is wide in range that water-insoluble VOCs content range in tail gas can be handled, adaptability
By force, the tail gas of all kinds of separate sources can be coped with extensively；Absorbent and purified water realization recycle, and avoid generating dangerous waste, and
Absorbent is water-soluble good, avoids generating secondary pollution to tail gas；Absorbent is recycled through regenerator and two step of recovery tower, reaches base
Basically no loss recycles, being capable of effectively save cost of material while environmental-friendly；Heat exchange processing between lean solution, rich solution
System thermal can be efficiently used, energy saving simplifies process route and promotes reaction efficiency.Process and item of the invention
Part is particularly suitable for the processing of the tail gas containing halogenated hydrocarbons, and water-insoluble VOCs content is lower than discharge in the tail gas of qualified discharge after processing
5~30mgm3 of standard-1。
Detailed description of the invention
The attached drawing for constituting a part of the invention is used to provide further understanding of the present invention, schematic reality of the invention
It applies example and its explanation is used to explain the present invention, do not constitute improper limitations of the present invention.In the accompanying drawings:
Fig. 1 is flow diagram of the invention.
Wherein, 1- tail gas absorber；2- rich solution pump；3- heat exchanger；4- solvent regeneration tower；5- solvent regeneration tower condenser；
6- solvent regeneration tower return tank, 7- solvent reclamation tower reboiler；8- lean pump；The first cooler of 9-；10- waste water pump；11- breaks tower
Disk；12- solvent recovery tower；13- solvent recovery tower condenser；14- solvent recovery tower return tank；The second cooler of 15-；16- is molten
Tower reboiler is recycled in agent；17- solvent recovery tower bottoms pump.
Specific embodiment
In order to better understand the present invention, present invention will now be described in detail with reference to the accompanying drawings..
Present invention design is as shown in Figure 1 containing water-insoluble VOCs tail gas treatment process process.Tail gas absorber 1 has top
Two sections of absorptions of water absorber portion and lower part solvent absorption section pass through disconnected tower tray 11 between two absorber portions and are isolated.Containing water-insoluble
The tail gas of VOCs enters the solvent absorption section bottom of tail gas absorber 1, is passed through absorbent, absorbent source at the top of solvent absorption section
The recycling design of lean solution and the extraction of 12 tower reactor of solvent recovery tower including the extraction of 4 tower reactor of solvent regeneration tower.Tail gas passes through solvent
Water absorber portion bottom is entered by disconnected tower tray 11 after the primary absorption of absorber portion inner absorbent, is passed through purification at the top of water absorber portion
Water.For tail gas from 1 top qualified discharge of tail gas absorber after purified water again absorption cleaning, purified water derives from solvent recovery
The water vapour produced at the top of tower 12 is condensed through cooling and is obtained.
1 bottom of tail gas absorber rich solution of the extraction containing water-insoluble VOCs enters rich solution pump 2, pressurization enter heat exchanger 3 with
Lean solution heat exchange enters 4 middle part of solvent regeneration tower after heating.Produced at the top of solvent regeneration tower 4 water-insoluble VOCs gas phase enter it is molten
Agent regenerator condenser 5 enters solvent regeneration tower return tank 6 after cooling, water-insoluble organic matter a part is as reflux in tank
Liquid is sent into 4 top of solvent regeneration tower, and another part is produced as water-insoluble organic matter product.The extraction of 4 tower reactor of solvent regeneration tower
Lean solution passes through the pressurization of lean pump 8 first and is sent into heat exchanger 3 and rich solution heat exchange, subsequently into the first further cooling of cooler 9, most
A part recycling at the top of the solvent absorption section of tail gas absorber 1 as absorbent is returned afterwards.
Waste water containing solvent is produced at the disconnected tower tray 11 of 1 water absorber portion of tail gas absorber, and solvent is sent by the pressurization of waste water pump 10
12 middle part of recovery tower.Water vapour is produced at the top of solvent recovery tower 12 and enters solvent recovery tower condenser 13, and solvent is entered after heat exchange
Recovery tower return tank 14, water a part is sent into 12 top of solvent recovery tower as phegma in tank, and it is cold that another part enters second
But recycling at the top of 1 water absorber portion of tail gas absorber is sent back to as purified water after device 15 cools down.12 tower reactor of solvent recovery tower is logical
17 extraction recycling design of solvent recovery tower bottoms pump is crossed, the solvent absorption of tail gas absorber 1 is returned as a part of absorbent
Section top.The total amount of recycling design is less relative to lean solution, therefore can be sent directly into tail gas absorber 1, can also be preferably
With after the lean solution cocurrent of heat exchanger 3 again through the first cooler 9 enter tail gas absorber 1, can also further preferably with
Successively enter tail gas absorber 1, figure through heat exchanger 3 and the first cooler 9 again after the lean solution cocurrent of 4 tower reactor of solvent regeneration tower extraction
It is exemplary in 1 to be shown as recycling design and enter tail gas absorber through the first cooler 9 again after the lean solution cocurrent of heat exchanger 3
1 process flow.
Use in the raw material tail gas of the present invention above-mentioned process processing water-insoluble VOCs content can for 100~
30000mg·m3-1, water-insoluble VOCs content is lower than 5~30mgm3 of discharge standard in the tail gas of qualified discharge after processing-1。
To meet different raw material operating conditions, process condition, which can according to need, to be adjusted, wherein absorbent with containing water-insoluble
The volume ratio of VOCs tail gas is 1:1000~1:10, and purified water is 1:1000~1 with water-insoluble VOCs exhaust gas volumes ratio is contained:
10；1 tower top operating pressure of tail gas absorber is 100~500PaA, and tower top operation temperature is 0~50 DEG C, and tower reactor operating pressure is
102~502PaA, tower reactor operation temperature are 0~50 DEG C；4 tower top operating pressure of solvent regeneration tower is 10~200KPaA, operation temperature
Degree is 30~150 DEG C, and tower reactor operating pressure is 12~202PaA, and tower reactor operation temperature is 120~195 DEG C；Solvent recovery tower 12
Top operating pressure is 10~300KPaA, and operation temperature is 80~190 DEG C, and tower reactor operating pressure is 12~302PaA, tower reactor operation
Temperature is 120~195 DEG C；Absorbent must be cooled to 5~50 DEG C before entering tail gas absorber 1.Reasonable optimization of process conditions mentions
High vent gas treatment and absorption efficiency, successfully manage different operating conditions, can especially adapt to the needs of the vent gas treatment containing halogenated hydrocarbons.
Below by taking certain pharmaceutical manufacturer's tail gas as an example, technique processing method of the invention is further illustrated.
Tail gas tolerance to be processed is 1000Nm3h-1, water-insoluble VOCs (halogenated hydrocarbons methylene chloride) content is
4000mg·m3-1, temperature is 30 DEG C.Tail gas to be processed is handled using above-mentioned process, each process main flow
And parameter is as follows:
1) it absorbs
Tail gas absorber 1 uses packed tower, D=1400mm, and solvent absorption section uses two sections of fillers, 7 meters of height.Water absorbs
Tri- sections of fillers of Duan Caiyong, 10 meters of packed height.
Use absorbent for 65% (v/v) DMSO, 35% (v/v) DMAc composition, internal circulating load 6m3h-1.Purified water follows
Circular rector is 3m3h-1。
30 DEG C of 1 tower top operation temperature of tail gas absorber, operating pressure 101KPaA.31 DEG C of tower reactor operation temperature, operation pressure
Power 104KPaA.Tail gas methylene chloride content after absorbing is lower than 30mgm3-1, meet the requirement of qualified discharge.
2) solvent reclamation
41 DEG C of 4 tower top operation temperature of solvent regeneration tower, operating pressure 101KPaA.190 DEG C of tower reactor operation temperature, operation
Pressure 104KPaA, reflux ratio 1.3.
3) solvent recovery
101 DEG C of 12 tower top operation temperature of solvent recovery tower, operating pressure 101KPaA.190 DEG C of tower reactor operation temperature, behaviour
Make pressure 103KPaA, reflux ratio 1.5.
To investigate influence of the different absorbents to vent gas treatment, the absorbent of different ratio is selected to handle tail containing methylene chloride
Gas, methylene chloride content is shown in Table 1 in finally obtained tail gas.
Table 1
As it can be seen from table 1 the composition of optimization absorbent can further decrease water-insoluble VOCs content in tail gas.
It is handled using method of the invention containing water-insoluble VOCs tail gas, water-insoluble VOCs absorption efficiency reaches
99.5% or more, water-insoluble VOCs content can be lower than 50mgm3 in emission-1, meet the requirement of qualified discharge.
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all in essence of the invention
Within mind and principle, any modification, equivalent replacement, improvement and so on be should all be included in the protection scope of the present invention.
Claims (10)
1. a kind of processing method containing water-insoluble VOCs tail gas, includes the following steps:
Using the tail gas absorber (1) with upper water absorber portion and lower part solvent absorption section, tail gas enters tail gas absorber (1)
Solvent absorption section, tail gas after the absorption of solvent absorption section inner absorbent enter water absorber portion, tail gas pass through water absorber portion
From tail gas absorber (1) top discharge after the absorption of interior purified water；
Tail gas absorber (1) bottom rich solution of the extraction containing water-insoluble VOCs passes through the lean solution produced with solvent regeneration tower (4) tower reactor
Heat exchange enters solvent regeneration tower (4), and water-insoluble VOCs gas phase, solvent regeneration tower (4) tower reactor are produced at the top of solvent regeneration tower (4)
The lean solution of extraction is through producing one after the rich solution containing water-insoluble VOCs exchanges heat as absorbent with tail gas absorber (1) bottom
Divide the solvent absorption section of return tail gas absorber (1)；
Tail gas absorber (1) water absorber portion bottom produces waste water containing solvent and is sent into solvent recovery tower (12), solvent recovery tower (12)
The water vapour condensation rear portion of top extraction returns to tail gas absorber (1) water absorber portion, solvent recovery tower as purified water
(12) tower reactor extraction recycling design returns to the solvent absorption section of tail gas absorber (1) as a part of absorbent.
2. the processing method according to claim 1 containing water-insoluble VOCs tail gas, which is characterized in that tail gas is inhaled from tail gas
The solvent absorption section bottom for receiving tower (1) enters, and absorbent is passed through from the top of solvent absorber portion, and purified water is logical from the top of water absorber portion
Enter；Rich solution containing water-insoluble VOCs enters solvent regeneration tower (4) from middle part, and waste water containing solvent enters solvent recovery tower from middle part
(12)；Pass through disconnected tower tray (11) isolation between two absorber portions of tail gas absorber (1)；Tail gas absorber (1), solvent regeneration tower
(4), the liquid between solvent recovery tower (12) is pressurizeed by force (forcing) pump and is transported；The solvent regeneration tower (4) and solvent recovery tower
(12) bottom further respectively has the reboiler for the vaporization that heats up.
3. the processing method according to claim 1 containing water-insoluble VOCs tail gas, which is characterized in that solvent regeneration tower
(4) for the water-insoluble VOCs gas phase that top produces after condensing, a part returns to solvent regeneration tower (4) as phegma, and one
It is allocated as the extraction of water-insoluble organic matter product；The water vapour condensation rear portion produced at the top of solvent recovery tower (12) is used as back
Flow liquid returns to solvent recovery tower (12).
4. the processing method according to claim 1 containing water-insoluble VOCs tail gas, which is characterized in that solvent recovery tower
(12) tower reactor extraction recycling design be sent directly into tail gas absorber (1), or with cooled down again after the lean solution cocurrent by heat exchange into
Enter tail gas absorber (1), or with solvent regeneration tower (4) tower reactor extraction lean solution cocurrent after successively exchanged heat again, cool down after enter
Tail gas absorber (1).
5. the processing method according to claim 1 containing water-insoluble VOCs tail gas, which is characterized in that non-in raw material tail gas
Water-soluble VOCs content is 100~30000mgm3-1, water-insoluble VOCs content is lower than in the tail gas of qualified discharge after processing
5~30mgm3 of discharge standard-1；
Absorbent and the volume ratio containing water-insoluble VOCs tail gas are 1:1000~1:10, purified water with contain water-insoluble VOCs tail
Air volume ratio is 1:1000~1:10；
Tail gas absorber (1) tower top operating pressure is 100~500PaA, and tower top operation temperature is 0~50 DEG C, tower reactor operating pressure
For 102~502PaA, tower reactor operation temperature is 0~50 DEG C；Solvent regeneration tower (4) tower top operating pressure is 10~200KPaA, behaviour
Making temperature is 30~150 DEG C, and tower reactor operating pressure is 12~202PaA, and tower reactor operation temperature is 120~195 DEG C；Solvent recovery
It is 10~300KPaA that tower (12), which pushes up operating pressure, and operation temperature is 80~190 DEG C, and tower reactor operating pressure is 12~302PaA, tower
Kettle operation temperature is 120~195 DEG C；Absorbent is cooled to 5~50 DEG C before entering tail gas absorber (1)；
The absorbent is water-soluble good organic solvent, or mixtures thereof pure component solvent including DMAc, NMP, DMSO,
One of solvent composition ratio is 5%~95%；The preferably mixture of DMSO, DMAc, wherein DMSO is in the mixture
Volume ratio is 65%-85%.
6. the processing method according to claim 1 containing water-insoluble VOCs tail gas, which is characterized in that described containing is non-aqueous
Dissolubility VOCs tail gas is tail gas containing halogenated hydrocarbons.
7. a kind of processing system containing water-insoluble VOCs tail gas, including tail gas absorber (1), solvent regeneration tower (4) and solvent
Recovery tower (12)；The tail gas absorber (1) has upper water absorber portion and lower part solvent absorption section, and solvent absorption section is equipped with tail
Gas feed inlet；All the way heat exchanger channels and solvent regeneration tower (4) of tail gas absorber (1) the bottom extraction mouth through heat exchanger (3)
Connection, solvent regeneration tower (4) tower reactor produce the solvent of another way heat exchanger channels and tail gas absorber (1) of the mouth through heat exchanger (3)
Absorber portion connection；Tail gas absorber (1) water absorber portion bottom extraction mouth is connected to solvent recovery tower (12), solvent recovery tower (12)
Top extraction mouth is connected to through solvent recovery tower condenser (13) with tail gas absorber (1) water absorber portion, solvent recovery tower (12) tower
Kettle extraction mouth is connected to the solvent absorption section of tail gas absorber (1).
8. processing system according to claim 7, which is characterized in that the tail gas feed inlet is set to tail gas absorber
(1) solvent absorption section bottom, solvent regeneration tower (4) tower reactor produce mouth and solvent recovery tower (12) tower reactor extraction mouth respectively with tail
The feed entrance point of the solvent absorption section connection of aspiration tower (1) is set at the top of the solvent absorption section of tail gas absorber (1), solvent
The feed entrance point that extraction mouth is connected to tail gas absorber (1) water absorber portion at the top of recovery tower (12) is set at the top of water absorber portion,
The feed entrance point that tail gas absorber (1) bottom extraction mouth is connected to solvent regeneration tower (4) is set in the middle part of solvent regeneration tower (4),
The feed entrance point that tail gas absorber (1) water absorber portion bottom extraction mouth is connected to solvent recovery tower (12) is set to solvent recovery tower
(12) middle part；Pass through disconnected tower tray (11) isolation between two absorber portions of tail gas absorber (1)；It adopts tail gas absorber (1) bottom
Outlet, solvent regeneration tower (4) tower reactor extraction mouth, tail gas absorber (1) water absorber portion bottom produce mouth, solvent recovery tower (12) tower
Force (forcing) pump is respectively arranged on the extraction pipeline of kettle extraction mouth；The solvent regeneration tower (4) and solvent recovery tower (12) bottom are also
It is respectively equipped with reboiler.
9. processing system according to claim 7, which is characterized in that extraction mouth is sequentially connected at the top of solvent regeneration tower (4)
There are solvent regeneration tower condenser (5), regenerator return tank (6), regenerator return tank (6) is equipped with and solvent regeneration tower (4) top
The return flow line of connection；Extraction mouth is connected with recovery tower condenser (13), solvent recovery tower in turn at the top of solvent recovery tower (12)
Return tank (14), solvent recovery tower return tank (14) are equipped with the return flow line being connected to solvent recovery tower (12) top, and solvent returns
It receives tower return tank (14) and is additionally provided with the solvent absorption section for making solvent recovery tower (12) tower reactor extraction mouth and tail gas absorber (1) all the way
The channel of connection.
10. processing system according to claim 7, which is characterized in that solvent recovery tower (12) tower reactor produce mouth directly with
The solvent absorption section of tail gas absorber (1) is connected to, or with exchange heat by heat exchanger (3) after pipeline cocurrent after again with tail gas absorption
The solvent absorption section of tower (1) is connected to, or with after the extraction pipeline cocurrent of solvent regeneration tower (4) tower reactor extraction mouth using heat exchanger
(3) it is then connected to the solvent absorption section of tail gas absorber (1)；Solvent regeneration tower (4) tower reactor produces mouth and solvent recovery tower
(12) it is additionally provided on the feed pipe for the feed entrance point that tower reactor extraction mouth is connected to the solvent absorption section of tail gas absorber (1) respectively
First cooler (9)；The feed entrance point that extraction mouth is connected to tail gas absorber (1) water absorber portion at the top of solvent recovery tower (12)
The second cooler (15) are additionally provided on feed pipe.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114425223A (en) * | 2020-10-15 | 2022-05-03 | 中国石油化工股份有限公司 | Tetrahydrofuran tail gas recovery system, method and application |
| CN114425219A (en) * | 2020-09-28 | 2022-05-03 | 中国石油化工股份有限公司 | Tetrahydrofuran tail gas treatment method, system and application |
| CN114887467A (en) * | 2022-05-26 | 2022-08-12 | 苏州璞赛环境科技有限公司 | Gas-phase sulfur dioxide tail gas treatment system and treatment method |
| CN115445392A (en) * | 2022-09-30 | 2022-12-09 | 上海化工研究院有限公司 | Recycling treatment process for chlorine-containing volatile organic compound waste gas |
| CN116392931A (en) * | 2023-05-15 | 2023-07-07 | 盐城优和博新材料有限公司 | System and method for treating tail gas generated in production of ultra-high-strength polyethylene fibers |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN86106882A (en) * | 1986-10-04 | 1987-07-22 | 辽宁省劳动保护科学研究所 | Purify the liquid-gas absorption process of containing benezene waste gas |
| TW457120B (en) * | 1999-11-17 | 2001-10-01 | Taiwan Semiconductor Mfg | Device and method for reducing volatile organic compound in exhaust |
| JP2008114203A (en) * | 2006-11-08 | 2008-05-22 | Nippon Refine Kk | Method and apparatus for recovering and enriching voc from voc-containing exhaust gas and cleaning exhaust gas |
| CN101439236A (en) * | 2008-12-12 | 2009-05-27 | 江苏迈克化工机械有限公司 | Device for executing recovery processing of organic discharge gas produced in coating procedure |
| JP2009241062A (en) * | 2008-03-13 | 2009-10-22 | Omega:Kk | Method for treating voc gas |
| CN104524929A (en) * | 2015-01-13 | 2015-04-22 | 天津奥展兴达化工技术有限公司 | Efficient energy-saving purification and recovery process of tail gas containing volatile organic compounds (VOCs) |
| CN105879619A (en) * | 2016-04-11 | 2016-08-24 | 江苏天晟环境科技有限公司 | VOCs (volatile organic compounds) tail gas treatment device and method |
| CN107715651A (en) * | 2017-10-17 | 2018-02-23 | 华南理工大学 | A kind of efficient low damage solvent for being used to absorb toluene and flow |
| CN108329208A (en) * | 2018-03-06 | 2018-07-27 | 华南理工大学 | A method of ethyl acetate is carried out using efficient low damage solvent to absorb processing |
| CN209333472U (en) * | 2018-12-27 | 2019-09-03 | 河北工业大学 | A kind of processing system containing water-insoluble VOCs tail gas |
-
2018
- 2018-12-27 CN CN201811612729.9A patent/CN109432955B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN86106882A (en) * | 1986-10-04 | 1987-07-22 | 辽宁省劳动保护科学研究所 | Purify the liquid-gas absorption process of containing benezene waste gas |
| TW457120B (en) * | 1999-11-17 | 2001-10-01 | Taiwan Semiconductor Mfg | Device and method for reducing volatile organic compound in exhaust |
| JP2008114203A (en) * | 2006-11-08 | 2008-05-22 | Nippon Refine Kk | Method and apparatus for recovering and enriching voc from voc-containing exhaust gas and cleaning exhaust gas |
| JP2009241062A (en) * | 2008-03-13 | 2009-10-22 | Omega:Kk | Method for treating voc gas |
| CN101439236A (en) * | 2008-12-12 | 2009-05-27 | 江苏迈克化工机械有限公司 | Device for executing recovery processing of organic discharge gas produced in coating procedure |
| CN104524929A (en) * | 2015-01-13 | 2015-04-22 | 天津奥展兴达化工技术有限公司 | Efficient energy-saving purification and recovery process of tail gas containing volatile organic compounds (VOCs) |
| CN105879619A (en) * | 2016-04-11 | 2016-08-24 | 江苏天晟环境科技有限公司 | VOCs (volatile organic compounds) tail gas treatment device and method |
| CN107715651A (en) * | 2017-10-17 | 2018-02-23 | 华南理工大学 | A kind of efficient low damage solvent for being used to absorb toluene and flow |
| CN108329208A (en) * | 2018-03-06 | 2018-07-27 | 华南理工大学 | A method of ethyl acetate is carried out using efficient low damage solvent to absorb processing |
| CN209333472U (en) * | 2018-12-27 | 2019-09-03 | 河北工业大学 | A kind of processing system containing water-insoluble VOCs tail gas |
Non-Patent Citations (1)
| Title |
|---|
| 邵昌哲;吕秋波;: "含丙酮等高浓VOCs废气的吸收工艺模拟优化设计", 化学工程与装备, no. 03, pages 289 - 292 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114425219A (en) * | 2020-09-28 | 2022-05-03 | 中国石油化工股份有限公司 | Tetrahydrofuran tail gas treatment method, system and application |
| CN114425223A (en) * | 2020-10-15 | 2022-05-03 | 中国石油化工股份有限公司 | Tetrahydrofuran tail gas recovery system, method and application |
| CN114887467A (en) * | 2022-05-26 | 2022-08-12 | 苏州璞赛环境科技有限公司 | Gas-phase sulfur dioxide tail gas treatment system and treatment method |
| CN115445392A (en) * | 2022-09-30 | 2022-12-09 | 上海化工研究院有限公司 | Recycling treatment process for chlorine-containing volatile organic compound waste gas |
| CN116392931A (en) * | 2023-05-15 | 2023-07-07 | 盐城优和博新材料有限公司 | System and method for treating tail gas generated in production of ultra-high-strength polyethylene fibers |
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