CN110252116A - A kind of recovery process based on flash distillation washing adsorption treatment styrene waste gases - Google Patents
A kind of recovery process based on flash distillation washing adsorption treatment styrene waste gases Download PDFInfo
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Abstract
The invention belongs to industrial waste gas recovery technology fields, and in particular to a kind of recovery process based on flash distillation washing adsorption treatment styrene waste gases.Recovery process of the present invention based on flash distillation washing adsorption treatment styrene waste gases, it is made of mixing, flash distillation, washing and absorption, it is capable of handling styrene waste gases caused by a variety of fields such as butylbenzene device exhaust, terminal ship and storage tank breathing, by mixing in exhaust gas 85%~95% recycling phenylethylene and flashing, it can be by exhaust gas 4%~15% recycling phenylethylene by washing, then absorbent and remaining part styrene are adsorbed by adsorbing, content of organics in tail gas is controlled in discharge standard hereinafter, to meet normal discharge.Styrene in exhaust gas can be farthest recycled by recovery process of the present invention, and realization is turned waste into wealth, while avoid the polymerization of styrene in absorbing process, and the even running of device is effectively ensured.
Description
Technical field
The invention belongs to industrial waste gas recovery technology fields, and in particular to one kind is based on flash distillation washing adsorption treatment styrene
The recovery process of exhaust gas.
Background technique
Styrene also known as vinyl benzene, Ethenylbenzene are a kind of colourless oily liquids to yellow transparent, belong to second level inflammable liquid
Body, steam meet high temperature or oxidant, there is the danger of combustion explosion.The most important purposes of styrene is used as synthetic rubber and modeling
The raw material of material, and homopolymer-polystyrene of styrene is even more one of five big general thermoplastic synthetic resins, is widely used in
The fields such as injection molding, extrusion and foamed product；Styrene can be also copolymerized with other monomers, for manufacturing with a variety of use
The engineering plastics on way, for example, the copolymer of styrene and butadiene is known as butadiene-styrene rubber, physical property, processing performance and system
The service performance of product is the largest general purpose synthetic rubber kind close to natural rubber, is widely used in tire, adhesive tape, sebific duct, electricity
The fields such as the production of line cable, medical apparatus and various rubber products；In addition, the Eprazinone of styrene or pharmaceutical industry, stomach
The bulk pharmaceutical chemicals of the drugs such as Changning also have a wide range of applications in field of medicaments.
But styrene is typical odor pollution substance, not only seriously pollutes environment, declines air quality, may be used also
Enter human body through number of ways such as respiratory tract, skin and gastrointestinal tracts, human health is caused great harm.In addition, benzene
Ethylene can also generate intense stimulus effect to eyes and the upper respiratory tract, make one to occur shedding tears, runny nose, cough, the discomforts such as sneezing
Sense, it is serious to even result in acute poisoning, generate the symptoms such as dizzy, headache, out of strength.
It is provided in the newest GB-1571 " petro chemical industry pollutant emission standard " issued of country, styrene in exhaust gas
Emission limit is 50mg/m3.Currently, domestic effective improvement to styrene waste gases is in the laboratory research stage mostly, row
Effective processing method is seen in the seldom of report, and since these methods are there are certain scope of application and limitation,
It is difficult to carry out comprehensively and is suitable for the styrene waste gases processing that Petrochemical Enterprises styrene is generated in the breathing of entrucking, shipment and storage tank.
Currently, the processing method of styrene waste gases mainly has condensation method and absorption method: condensation method can direct recovering liquid benzene
Ethylene, but condensation method reaches environmental protection standard needs and drops to very low temperature, causes energy consumption higher and device configuration is complicated, it is tired to safeguard
It is difficult；And absorption method processing styrene waste gases mostly use greatly acticarbon, but have easily polymerization, polymerization thermal effect in view of styrene
Long-time service activated carbon adsorption should be caused to easily cause active carbon inactivation that can not regenerate and have fire with the absorption biggish problem of fuel factor
Calamity risk.
If Chinese patent CN204543913U discloses a kind of recycling phenylethylene system, by setting condenser come to tail gas
It liquefies to facilitate and be separated to styrene, the tail gas after liquefying can be collected in degassing collecting tank, wait be collected into one
Re-liquefied Tail Gas is passed through in oil water separator again after fixed amount, realization styrene is separated from water and the purification of styrene.But
The scope of application of the styrene processing system is extremely limited, and process is complex.
For another example Chinese patent CN102527185A discloses a kind of method by modified meerschaum absorption styrene waste gases, benefit
Modified sea with the modified meerschaum in adsorption tower in 0~80 DEG C of adsorbable foul waste gas containing styrene, after adsorption saturation
Afrodite can recycle benefit after sepiolite regeneration through condensing recovery in 150~350 DEG C of desorption styrene in situ, the styrene of high concentration
With.But preparing for the modified afrodite of this method is complex, and its desorption temperature is higher, and there are certain security risks.
For another example patent CN105344224A discloses a kind of styrene waste gases processing method, utilizes styrene waste gases and Gao Meng
The alkaline solution of sour potassium carries out counter current contacting, and oxidation occurs for the alkaline solution of styrene and potassium permanganate anti-in contact process
It answers, the exhaust gas for consuming styrene after the reaction was completed is discharged into atmosphere.The technique can realize the removing of styrene in exhaust gas, still
The MnO generated after the alkaline solution reduction of potassium permanganate2Equal solid matters do not have good treatment process.
As it can be seen that developing, a kind of recovery efficiency is high and the recycling phenylethylene technique of safety and stability, is not only production of styrene neck
Urgent problem to be solved in domain, with more biggish industry and environment protection significance.
Summary of the invention
For this purpose, a kind of useless based on flash distillation washing adsorption treatment styrene technical problem to be solved by the present invention lies in providing
The recovery process of gas, to solve the problems, such as to cause environmental pollution because styrene waste gases recycle difficulty in the prior art.
In order to solve the above technical problems, a kind of returning based on flash distillation washing adsorption treatment styrene waste gases of the present invention
Knock off skill, includes the following steps:
(1) styrene waste gases and absorbent are sufficiently mixed, and mixed material is subjected to flash separation, obtained
Gaseous phase materials and liquid phase material；
(2) gained gaseous phase materials are mixed with cleaning solution and is washed, further recycle the styrene and organic in tail gas
Solvent；Resulting liquid phase material is then recycled；
(3) gas material after washing is subjected to adsorption treatment, further removes the organic matter in tail gas, and will be after absorption
Exhaust emissions；
(4) washed treated cleaning solution then carries out feed separation processing, and by after separation oil phase material and washing
Liquid is recycled respectively.
Specifically, the absorbent includes dimethylformamide, benzene, toluene, ethylbenzene, dimethyl second in the step (1)
In amide, ortho-xylene, paraxylene, meta-xylene, dimethyl sulfoxide, ethylene glycol, drippolene or de-pentane oil at least
It is a kind of.More preferably ortho-xylene, ethylbenzene, paraxylene, meta-xylene, drippolene, de-pentane oil or five mixing
Object, wherein the content of ortho-xylene, paraxylene and meta-xylene is respectively 0~100%, and drippolene, de-pentane oil contain
Amount is 0~40%.
Specifically, in the step (1), the mass volume ratio of the absorbent and the styrene tail gas is 0.033~
0.4kg/cum, the temperature for controlling the mixing step is 30~90 DEG C, and pressure is 0~10atm.It is furthermore preferred that the absorbent
Mass volume ratio with the styrene tail gas is 0.17~0.3kg/cum, and the temperature for controlling the mixing step is 30~50
DEG C, pressure is 3~6atm.
The specific mixing step carries out in a mixer, and the mixer can be mixed for static mixer, venturi
Clutch, pipe-line mixer and blending tank, and preferably venturi mixer and pipe-line mixer.
When selecting venturi mixer, selects trunnion section diameter and import and export the ratio range of diameter to be 0~1, shrink
Segment length range and inlet and outlet lenth ratio range be 0~1, expanding reach length range and inlet and outlet lenth ratio range be 0~
1.The ratio preferred scope of the trunnion section diameter and inlet and outlet diameter that more preferably select venturi mixer is 0.1~0.4, is received
Contracting segment length range and inlet and outlet lenth ratio preferred scope are 0.2~0.4, expanding reach length range and inlet and outlet lenth ratio
Range is 0.3~0.7.
When selecting pipe-line mixer, the diameter range of pipe-line mixer is 0~0.9m, the ratio range of length and diameter
0~20, the preferred 0.3~0.6m of diameter range for selecting pipe-line mixer, the ratio range 7~14 of length and diameter.
Specifically, the temperature of the flash steps is -30~90 DEG C in the step (1), pressure is 0~10atm.More
Preferably, the temperature of the flash steps is 20~40 DEG C, and pressure is 3~7atm.
Specifically, the cleaning solution is water, the cleaning solution and the gaseous phase materials containing styrene in the step (2)
Mass volume ratio be 0.04~0.7kg/cum.It is furthermore preferred that the mass volume ratio of the cleaning solution and the styrene tail gas
For 0.15~0.4kg/cum.
Specifically, the temperature of the washing step is 0~90 DEG C in the step (2), pressure is 0~10atm.It is more excellent
Choosing, the temperature of the washing step is 20~40 DEG C, and pressure is 3~6atm.
Specifically, in resulting liquid phase material, Partial Liquid Phase material recycle is recycled as absorbent in the step (2)
It uses, rest part liquid phase material then recycles.
Specifically, controlling institute it is characterized in that, the washing step is carried out in scrubbing tower in the step (2)
The number of plates for stating scrubbing tower is 2~22, and preferably 5~14 pieces.The scrubbing tower can be packed tower and plate column.
Specifically, carrying out organic solvent in gaseous phase materials using adsorbent in the adsorption step in the step (3)
Removing；The adsorbent includes active carbon, X-type molecular sieve, 5A type molecular sieve or diatomite.Most preferably active carbon and X-type point
Son sieve.
Specifically, the temperature of the adsorption step is 0~90 DEG C in the step (3), pressure is 0~6atm, and absorption is empty
Speed is 0~8h-1.More preferably, control adsorption temp is 30~60 DEG C, and pressure is 1~3atm, and absorption air speed is 1~4h1。
Specifically, further including the steps that being recycled the oil phase material as absorbent in the step (4)；With
And the step of cleaning solution is recycled.
It is of the present invention based on flash distillation washing adsorption treatment styrene waste gases recovery process, by mixing, flash distillation, washing and
Absorption composition is capable of handling useless containing styrene caused by a variety of fields such as butylbenzene device exhaust, terminal ship and storage tank breathing
Gas can be by exhaust gas 4%~15% by washing by mixing in exhaust gas 85%~95% recycling phenylethylene and flashing
Recycling phenylethylene is then adsorbed absorbent and remaining part styrene by adsorbing, by the organic exhaust gas in tail gas
Content control is in discharge standard hereinafter, to meet normal discharge.Recovery process of the present invention can farthest will be in exhaust gas
Styrene be recycled, realization is turned waste into wealth, while avoiding the polymerization of styrene in absorbing process, and device is effectively ensured
Even running.
Detailed description of the invention
In order to make the content of the present invention more clearly understood, it below according to specific embodiments of the present invention and combines
Attached drawing, the present invention is described in further detail, wherein
Fig. 1 is the device flow diagram of recovery process of the present invention；
Appended drawing reference indicates in figure are as follows: 1- mixer, 2- flash tank, 3- scrubbing tower, 4- adsorptive reactor, 5- water-oil separating
Device, 6- styrene waste gases, 7- absorbent, 8- gaseous phase materials, 9- liquid phase material, 10- cleaning solution, 11- oil phase, 12- water phase, 13-
Tail gas.
Specific embodiment
Process unit schematic diagram as shown in Figure 1 realizes that the device of recovery process of the present invention includes sequential communication
Mixer 1, flash tank 2, scrubbing tower 3, adsorptive reactor 4 and oil water separator 5.
Recovery scheme described in the following embodiments of the present invention, when carrying out the recycling of styrene waste gases, styrene waste gases 6 with
The absorbent 7 of selection is sufficiently mixed in mixer 1, and mixed material is entered flash tank 2 and carries out flash distillation process；
Material is after flash separation, and the gaseous phase materials 8 positioned at 2 tower top of flash tank are washed into scrubbing tower 3, and isolated liquid phase
In material 9, Partial Liquid Phase returns to mixer 1 and reuses as absorbent, and remainder liquid phase is then returned as high-value product
It receives and utilizes；The gaseous phase materials 8 enter scrubbing tower 3 from tower bottom, cleaning solution 10 (water) counter current contacting on tower tray with tower top, lead to
It crosses the styrene washed by tail gas and organic solvent recycles, the gaseous phase materials positioned at 3 tower top of scrubbing tower can enter absorption
Reactor 4 is removed the organic matter in tail gas by adsorbent, to guarantee 13 qualified discharge of tail gas；And it is located at scrubbing tower 3
The liquid phase material (the mainly mixture of water, styrene and absorbent) of tower bottom then enters oil water separator 5, by static layering
Afterwards, oily phase 11 located above can return to mixer 1 and reuse as absorbent, and the water phase 12 for being located at lower layer is then returned to and washed
The tower top for washing tower 3 is reused as cleaning solution.
Embodiment 1
Styrene waste gases are in the present embodiment with four 5000m3Styrene storage tank, and be internal floating roof tank, pass through breathing
The exhaust flow of hole discharge is 3000m3/ h, styrene-content therein are 6000ppm, remaining is air.
Recovery process described in the present embodiment is recycled using such as attached device shown in FIG. 1.
In the mixer 1, using pipe-line mixer, the diameter for controlling pipe-line mixer is 0.4m, the length of mixer
For 4m, using ortho-xylene as absorbent, control mixer temperature is 32 DEG C, and the flow of control mixer absorbent is 800kg/
h。
In the flash tank 2, controlled at 30 DEG C, pressure 3.9atm.2 top gaseous phase of flash tank carries out scrubbing tower 3,
In 2 bottom liquid phases of flash tank, 90%, which returns to mixer 1, is used as absorbent, and in addition 10% recycles.
The scrubbing tower 3 is packed tower, and number of theoretical plate 8, tower top temperature is 30 DEG C, and the flow of control absorbing tower water is
800kg/h。
In the adsorptive reactor 4, using active carbon as adsorbent, control gas phase air speed is 2h-1。
In the present embodiment, after the processing of above-mentioned recovery process, in the gaseous phase materials and liquid phase material that each device part is related to
The variation of styrene and absorbent contents is as shown in table 1.
The content of organic matter in 1 embodiment of table, 1 gas phase and liquid phase
By upper 1 data of table it is found that the styrene in tail gas after treatment is reduced to 35ppm, styrene by 6000ppm
The rate of recovery be 99.42%, at this point, the content of ortho-xylene be 430ppm, be computed, by raw material absorb bring benefit be about
7666 yuan；And after whole adsorption treatments, in tail gas, the total content of styrene and ortho-xylene is only 23ppm, meets discharge
Standard.
Comparative example 1
Styrene waste gases are in this comparative example with four 5000m3Styrene storage tank, be internal floating roof tank, pass through spiracle
The exhaust flow of discharge is 3000m3/ h, styrene-content therein are 6000ppm, remaining is air.
Recovery process described in this comparative example is recycled using such as attached device shown in FIG. 1.
In the mixer 1, using pipe-line mixer, the diameter for controlling pipe-line mixer is 1m, and the length of mixer is
10m, using ortho-xylene as absorbent, control mixer temperature is 32 DEG C, and the flow of control mixer absorbent is 800kg/
h。
In the flash tank 2, controlled at 30 DEG C, pressure 3.9atm.2 top gaseous phase of flash tank carries out scrubbing tower 3,
In 2 bottom liquid phases of flash tank, 90%, which returns to mixer 1, is used as absorbent, and in addition 10% recycles.
The scrubbing tower 3 is packed tower, and number of theoretical plate 8, tower top temperature is 30 DEG C, and the flow of control absorbing tower water is
800kg/h。
In the adsorptive reactor 4, using active carbon as adsorbent, control gas phase air speed is 2h-1。
In this comparative example, after the processing of above-mentioned recovery process, in the gaseous phase materials and liquid phase material that each device part is related to
The variation of styrene and absorbent contents is as shown in table 2.
The content of organic matter in 2 gas phase of table and liquid phase
By upper 2 data of table it is found that compared with 1 scheme of embodiment, in the case where remaining process conditions is constant, pipeline mixing
The diameter of device increases to 1m, and mixed effect can be deteriorated, and the content for flashing styrene in head space gas phase is increased to by 320ppm
1250ppm, styrene-content increases to 450ppm by 35ppm in corresponding scrubbing tower top gaseous phase, and styrene contains in tail gas
The content far more than discharge standard styrene is measured, it can not direct emission.
Embodiment 2
Styrene waste gases are in the present embodiment with four 5000m3Styrene storage tank, be internal floating roof tank, pass through spiracle
The exhaust flow of discharge is 3000m3/ h, styrene-content therein are 2000ppm, remaining is air.
Recovery process described in the present embodiment is recycled using such as attached device shown in FIG. 1.
In the mixer 1, using pipe-line mixer, the diameter for controlling pipe-line mixer is 0.4m, the length of mixer
For 4m, using ortho-xylene as absorbent, mixer temperature is 32 DEG C, and the flow of control mixer absorbent is 800kg/h.
In the flash tank 2, controlled at 30 DEG C, pressure 3.9atm.2 top gaseous phase of flash tank carries out scrubbing tower 3,
In 2 bottom liquid phases of flash tank, 90%, which returns to mixer 1, is used as absorbent, and in addition 10% recycles.
The scrubbing tower 3 is packed tower, and number of theoretical plate 8, tower top temperature is 30 DEG C, and the flow of control absorbing tower water is
800kg/h。
In the adsorptive reactor 4, using active carbon as adsorbent, control gas phase air speed is 2h-1。
In the present embodiment, after the processing of above-mentioned recovery process, in the gaseous phase materials and liquid phase material that each device part is related to
The variation of styrene and absorbent contents is as shown in table 3.
The content of organic matter in 3 gas phase of table and liquid phase
From the data in table 3, it can be seen that the styrene in tail gas after treatment is reduced to 1ppm by 2000ppm, styrene
The rate of recovery is 99.95%, at this point, the content of ortho-xylene is 320ppm, absorbing bring benefit by raw material is about 7015 yuan；And
After whole adsorption treatments, the total content of styrene and ortho-xylene is 12ppm in tail gas, meets discharge standard.
Comparative example 2-1
Styrene waste gases are in this comparative example with four 5000m3Styrene storage tank, be internal floating roof tank, pass through spiracle
The exhaust flow of discharge is 3000m3/ h, styrene-content therein are 2000ppm, remaining is air.
Recovery process described in this comparative example is recycled using such as attached device shown in FIG. 1.
In the mixer 1, using pipe-line mixer, the diameter for controlling pipe-line mixer is 0.4m, the length of mixer
For 4m, using ortho-xylene as absorbent, mixer temperature is 32 DEG C, and the flow of control mixer absorbent is 400kg/h.
In the flash tank 2, controlled at 30 DEG C, pressure 3.9atm.2 top gaseous phase of flash tank carries out scrubbing tower 3,
In 2 bottom liquid phases of flash tank, 90%, which returns to mixer 1, is used as absorbent, and in addition 10% recycles.
The scrubbing tower 3 is packed tower, and number of theoretical plate 8, tower top temperature is 30 DEG C, and the flow of control absorbing tower water is
800kg/h。
The adsorptive reactor 4, using active carbon as adsorbent, control gas phase air speed is 2h-1。
In this comparative example, after the processing of above-mentioned recovery process, in the gaseous phase materials and liquid phase material that each device part is related to
The variation of styrene and absorbent contents is as shown in table 4.
The content of organic matter in 4 gas phase of table and liquid phase
From the data in table 4, it can be seen that, in the case where remaining process conditions is constant, mixer absorbs compared with 2 scheme of embodiment
The flow of agent is reduced to 400kg/h by 800kg/h, and mixed effect is deteriorated, and flashes the content of styrene in head space gas phase by 85ppm
Increase to 435ppm, styrene-content increases to 225ppm, styrene in tail gas by 1ppm in corresponding scrubbing tower top gaseous phase
Content 79ppm can not direct emission more than the content of styrene in discharge standard.
Comparative example 2-2
Styrene waste gases are in this comparative example with four 5000m3Styrene storage tank, be internal floating roof tank, pass through spiracle
The exhaust flow of discharge is 3000m3/ h, styrene-content therein are 2000ppm, remaining is air.
Recovery process described in this comparative example is recycled using such as attached device shown in FIG. 1.
In the mixer 1, using pipe-line mixer, the diameter for controlling pipe-line mixer is 0.4m, the length of mixer
For 4m, using benzene as absorbent, mixer temperature is 32 DEG C, and the flow of control mixer absorbent is 800kg/h.
In the flash tank 2, controlled at 30 DEG C, pressure 3.9atm.2 top gaseous phase of flash tank carries out scrubbing tower 3,
In 2 bottom liquid phases of flash tank, 90%, which returns to mixer 1, is used as absorbent, and in addition 10% recycles.
The scrubbing tower 3 is packed tower, and number of theoretical plate 8, tower top temperature is 30 DEG C, and the flow of control absorbing tower water is
800kg/h。
The adsorptive reactor 4, using active carbon as adsorbent, control gas phase air speed is 2h-1。
In this comparative example, after the processing of above-mentioned recovery process, in the gaseous phase materials and liquid phase material that each device part is related to
The variation of styrene and absorbent contents is as shown in table 5.
The content of organic matter in 5 gas phase of table and liquid phase
From the data in table 5, it can be seen that, in the case where remaining process conditions is constant, being replaced compared with 2 scheme of embodiment with benzene adjacent
Dimethylbenzene is basically unchanged as absorbent, mixed effect and assimilation effect, flashes the content of styrene in head space gas phase by 85ppm
It is reduced to 74ppm, styrene-content is constant in scrubbing tower top gaseous phase.But the content of benzene increases obvious, flash tank in gas phase
Benzene content has 10000ppm to increase to 110000ppm in top gas phase, and benzene content is increased to by 203ppm in scrubbing tower top gaseous phase
10230ppm, benzene content by 12ppm increases to 2345ppm in adsorptive reactor outlet gas phase, is unable to satisfy discharge standard, simultaneously
The technique does not have economy.
Embodiment 3
Styrene waste gases are in the present embodiment with four 5000m3Styrene storage tank, be internal floating roof tank, pass through spiracle
The exhaust flow of discharge is 3000m3/ h, styrene-content therein are 3000ppm, remaining is air.
Recovery process described in the present embodiment is recycled using such as attached device shown in FIG. 1.
In the mixer 1, using pipe-line mixer, the diameter for controlling pipe-line mixer is 0.4m, the length of mixer
For 4m, using ortho-xylene as absorbent, mixer temperature is 32 DEG C, and the flow of control mixer absorbent is 800kg/h.
In the flash tank 2, controlled at 30 DEG C, pressure 3.9atm.2 top gaseous phase of flash tank carries out scrubbing tower 3,
In 2 bottom liquid phases of flash tank, 90%, which returns to mixer 1, is used as absorbent, and in addition 10% recycles.
The scrubbing tower 3 is packed tower, and number of theoretical plate 8, tower top temperature is 30 DEG C, and the flow of control absorbing tower water is
800kg/h。
The adsorptive reactor 4, using active carbon as adsorbent, control gas phase air speed is 2h-1。
In the present embodiment, after the processing of above-mentioned recovery process, in the gaseous phase materials and liquid phase material that each device part is related to
The variation of styrene and absorbent contents is as shown in table 6.
The content of organic matter in 6 gas phase of table and liquid phase
From the data in table 6, it can be seen that after treatment, the styrene in tail gas is reduced to 12ppm by 3000ppm, styrene
The rate of recovery is 99.6%, and the content of ortho-xylene is 324ppm at this time, and absorbing bring benefit by raw material is about 7397 yuan；By
After whole adsorption treatments, the content of styrene and ortho-xylene is 15ppm in tail gas, meets discharge standard.
Comparative example 3-1
Styrene waste gases are in this comparative example with four 5000m3Styrene storage tank, be internal floating roof tank, pass through spiracle
The exhaust flow of discharge is 3000m3/ h, styrene-content therein are 3000ppm, remaining is air.
Recovery process described in this comparative example is recycled using such as attached device shown in FIG. 1.
In the mixer 1, using pipe-line mixer, the diameter for controlling pipe-line mixer is 0.4m, the length of mixer
For 4m, using ortho-xylene as absorbent, mixer temperature is 32 DEG C, and the flow of control mixer absorbent is 800kg/h.
In the flash tank 2, controlled at 30 DEG C, pressure 3.9atm.2 top gaseous phase of flash tank carries out scrubbing tower 3,
In 2 bottom liquid phases of flash tank, 90%, which returns to mixer 1, is used as absorbent, and in addition 10% recycles.
The scrubbing tower is packed tower, and number of theoretical plate 8, tower top temperature is 30 DEG C, and the flow of control absorbing tower water is
400kg/h。
The adsorptive reactor, using active carbon as adsorbent, control gas phase air speed is 2h-1。
In this comparative example, after the processing of above-mentioned recovery process, in the gaseous phase materials and liquid phase material that each device part is related to
The variation of styrene and absorbent contents is as shown in table 7.
The content of organic matter in 7 gas phase of table and liquid phase
From the data in table 7, it can be seen that this comparative example scheme is after treatment, the styrene in tail gas is reduced to by 3000ppm
38ppm, the rate of recovery of styrene are 98.7%, and the content of ortho-xylene is 724ppm at this time, absorb bring benefit by raw material
About 6391 yuan.Since the dosage of water reduces in the embodiment, the content of styrene and ortho-xylene in scrubbing tower top gaseous phase
It obviously increases, causes the content of styrene and ethylbenzene in tail gas exceeded, be unable to satisfy discharge standard.
Comparative example 3-2
Styrene waste gases are in this comparative example with four 5000m3Styrene storage tank, be internal floating roof tank, pass through spiracle
The exhaust flow of discharge is 3000m3/ h, styrene-content therein are 3000ppm, remaining is air.
Recovery process described in this comparative example is recycled using such as attached device shown in FIG. 1.
In the mixer 1, using pipe-line mixer, the diameter for controlling pipe-line mixer is 0.4m, the length of mixer
For 4m, using ortho-xylene as absorbent, mixer temperature is 32 DEG C, and the flow of control mixer absorbent is 800kg/h.
In the flash tank 2, controlled at 30 DEG C, pressure 3.9atm.2 top gaseous phase of flash tank carries out scrubbing tower 3,
In 2 bottom liquid phases of flash tank, 90%, which returns to mixer 1, is used as absorbent, and in addition 10% recycles.
The scrubbing tower 3 is packed tower, and number of theoretical plate 8, tower top temperature is 30 DEG C, and the flow of control absorbing tower water is
800kg/h。
The adsorptive reactor 4, using active carbon as adsorbent, control gas phase air speed is 5h-1。
In this comparative example, after the processing of above-mentioned recovery process, in the gaseous phase materials and liquid phase material that each device part is related to
The variation of styrene and absorbent contents is as shown in table 8.
The content of organic matter in 8 gas phase of table and liquid phase
From the data in table 8, it can be seen that this comparative example scheme is after treatment, the styrene in tail gas is reduced to by 3000ppm
12ppm, the rate of recovery of styrene are 99.6%, and the content of ortho-xylene is 724ppm at this time, absorb bring benefit by raw material
About 7397 yuan.Since adsorptive reactor air speed is by 2h in the comparative example-1Increase to 5h-1, adsorptive reactor export gas phase in benzene
The content of ethylene and ortho-xylene obviously increases, and causes the content of styrene and ethylbenzene in tail gas exceeded, is unable to satisfy discharge mark
It is quasi-.
Obviously, the above embodiments are merely examples for clarifying the description, and does not limit the embodiments.It is right
For those of ordinary skill in the art, can also make on the basis of the above description it is other it is various forms of variation or
It changes.There is no necessity and possibility to exhaust all the enbodiments.And it is extended from this it is obvious variation or
It changes still within the protection scope of the invention.
Claims (10)
1. a kind of recovery process based on flash distillation washing adsorption treatment styrene waste gases, which comprises the steps of:
(1) styrene waste gases and absorbent are sufficiently mixed, and mixed material is subjected to flash separation, obtain gas phase
Material and liquid phase material；
(2) gained gaseous phase materials are mixed with cleaning solution and is washed, further recycle the styrene and organic solvent in tail gas；
Resulting liquid phase material is then recycled；
(3) gas material after washing is subjected to adsorption treatment, further removes the organic matter in tail gas, and by the tail after absorption
Gas discharge；
(4) washed treated cleaning solution then carries out feed separation processing, and by the oil phase material and cleaning solution point after separation
It is not recycled.
2. the recovery process according to claim 1 based on flash distillation washing adsorption treatment styrene waste gases, which is characterized in that
In the step (1), the absorbent include dimethylformamide, benzene, toluene, ethylbenzene, dimethyl acetamide, ortho-xylene,
At least one of paraxylene, meta-xylene, dimethyl sulfoxide, ethylene glycol, drippolene or de-pentane oil.
3. the recovery process according to claim 1 or 2 based on flash distillation washing adsorption treatment styrene waste gases, feature exist
In in the step (1), the mass volume ratio of the absorbent and the styrene tail gas is 0.033~0.4kg/cum, control
The temperature for making the mixing step is 30~90 DEG C, and pressure is 0~10atm.
4. described in any item recovery process based on flash distillation washing adsorption treatment styrene waste gases according to claim 1~3,
It is characterized in that, in the step (1), the temperature of the flash steps is 30~90 DEG C, and pressure is 0~10atm.
5. the recovery process according to any one of claims 1 to 4 based on flash distillation washing adsorption treatment styrene waste gases,
It is characterized in that, in the step (2), the cleaning solution is water, the quality of the cleaning solution and the gaseous phase materials containing styrene
Volume ratio is 0.04~0.7kg/cum；The temperature of the washing step is 0~90 DEG C, and pressure is 0~10atm.
6. described in any item recovery process based on flash distillation washing adsorption treatment styrene waste gases according to claim 1~5,
It being characterized in that, in the step (2), in resulting liquid phase material, Partial Liquid Phase material recycle is recycled as absorbent,
Remaining part liquid separation phase materials then recycle.
7. described in any item recovery process based on flash distillation washing adsorption treatment styrene waste gases according to claim 1~6,
It is characterized in that, in the step (2), the washing step is carried out in scrubbing tower, controls the number of plates of the scrubbing tower
It is 2~22.
8. described in any item recovery process based on flash distillation washing adsorption treatment styrene waste gases according to claim 1~7,
It is characterized in that, in the step (3), carries out the removing of organic solvent in gaseous phase materials in the adsorption step using adsorbent；
The adsorbent includes active carbon, X-type molecular sieve, 5A type molecular sieve or diatomite.
9. described in any item recovery process based on flash distillation washing adsorption treatment styrene waste gases according to claim 1~8,
It is characterized in that, in the step (3), the temperature of the adsorption step is 0~90 DEG C, and pressure is 0~6atm, and absorption air speed is 0
~8h-1。
10. described in any item recovery process based on flash distillation washing adsorption treatment styrene waste gases according to claim 1~9,
It is characterized in that, further including the steps that being recycled the oil phase material as absorbent in the step (4)；And it will
The step of cleaning solution is recycled.
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| CN116585856A (en) * | 2023-06-21 | 2023-08-15 | 无锡海霖格科技有限公司 | Volatile organic compound absorbent, preparation method thereof and absorption system |
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