CN109731433A - The ethyl acetate recovery method combined is adsorbed with runner using activated carbon adsorption - Google Patents
The ethyl acetate recovery method combined is adsorbed with runner using activated carbon adsorption Download PDFInfo
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- CN109731433A CN109731433A CN201811545556.3A CN201811545556A CN109731433A CN 109731433 A CN109731433 A CN 109731433A CN 201811545556 A CN201811545556 A CN 201811545556A CN 109731433 A CN109731433 A CN 109731433A
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- carbon adsorption
- active carbon
- runner
- desorption
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 177
- 238000001179 sorption measurement Methods 0.000 title claims abstract description 149
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 title claims abstract description 57
- 238000000034 method Methods 0.000 title claims abstract description 36
- 238000011084 recovery Methods 0.000 title claims abstract description 25
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 103
- 238000003795 desorption Methods 0.000 claims abstract description 61
- 238000010521 absorption reaction Methods 0.000 claims abstract description 38
- 230000008929 regeneration Effects 0.000 claims abstract description 32
- 238000011069 regeneration method Methods 0.000 claims abstract description 32
- 239000006096 absorbing agent Substances 0.000 claims abstract description 23
- 239000002904 solvent Substances 0.000 claims abstract description 18
- 239000007789 gas Substances 0.000 claims description 79
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 16
- 238000009833 condensation Methods 0.000 claims description 9
- 230000005494 condensation Effects 0.000 claims description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 8
- 229910052757 nitrogen Inorganic materials 0.000 claims description 8
- 239000001301 oxygen Substances 0.000 claims description 8
- 229910052760 oxygen Inorganic materials 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 6
- 230000001172 regenerating effect Effects 0.000 claims description 5
- 238000001914 filtration Methods 0.000 claims description 2
- 239000003960 organic solvent Substances 0.000 claims description 2
- 239000003063 flame retardant Substances 0.000 claims 3
- 238000006073 displacement reaction Methods 0.000 claims 1
- 230000008439 repair process Effects 0.000 claims 1
- 230000035899 viability Effects 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 19
- 238000010926 purge Methods 0.000 abstract description 3
- 230000008676 import Effects 0.000 abstract 1
- 239000003610 charcoal Substances 0.000 description 15
- 238000004064 recycling Methods 0.000 description 5
- 239000002351 wastewater Substances 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 4
- 238000007664 blowing Methods 0.000 description 3
- 239000012855 volatile organic compound Substances 0.000 description 3
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000035425 carbon utilization Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 239000010457 zeolite Substances 0.000 description 2
- OKTJSMMVPCPJKN-IGMARMGPSA-N Carbon-12 Chemical class [12C] OKTJSMMVPCPJKN-IGMARMGPSA-N 0.000 description 1
- 208000012287 Prolapse Diseases 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- XYIBRDXRRQCHLP-UHFFFAOYSA-N ethyl acetoacetate Chemical compound CCOC(=O)CC(C)=O XYIBRDXRRQCHLP-UHFFFAOYSA-N 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 239000012774 insulation material Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 238000007639 printing Methods 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
- 230000001755 vocal effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The ethyl acetate recovery method combined is adsorbed with runner using activated carbon adsorption the present invention provides a kind of, it is combined by using three or more absorbers with runner absorber, the adsorption rate of ethyl acetate in the exhaust system of middle and high concentration is increased to 99.5% or more.Primary activity canister after adsorption saturation first adsorbs the regeneration for carrying out solvent rich, completing primary activity canister through second order activity canister, and second order activity canister inversely purges regeneration through inert hot gas again, is taken to liquefy in condenser by desorption blower and be recycled.The ethyl acetate of runner absorption is regenerated back to exhaust system import by hot wind, completes the regeneration of runner.This method is combined by active carbon with runner absorption, while guaranteeing tail gas qualified discharge, is realized the circular regeneration of system, is greatly improved the rate of recovery of solvent.
Description
Technical field
The method that mode recycles ethyl acetate is combined with runner absorption using activated carbon adsorption the present invention relates to a kind of, it is living
Property charcoal using second level tank is enriched with, thermal inertia gas is regenerated, regeneration gas condensation uses chilled water, is applied especially to insulation material
The processing of organic exhaust gas in material, reflectorized material and printing industry.
Background technique
It is suitable for the absorption of middle low concentration tail gas 201210299494.9 being adsorbed using single-stage Activated Carbon toward VOCs-Containing Exhausts
Processing will appear after activated carbon adsorption certain time, concentration of emission reach predetermined value and discharge problem not up to standard, active carbon
Adsorb that switching cycle is shorter, in switching active carbon degree of saturation is low, active carbon utilization rate is low；The regenerating active carbon of this method
Process is utilized second order activity canister and is enriched with to organic solvent, reduces primary activity canister desorption and remains, and the two of this method
Grade charcoal canister is not fixed as some tank, but switches in turn between three or more charcoal canisters.
201611246859.6 come recycling design in such a way that active carbon is combined with runner absorption.Utilize 2 activity
Canister, another desorption of an absorption, the regeneration desorption of this method active carbon directly add active carbon bed using steam
The mode of heat, the water and solvent mixed liquor that desorption condensation generates are layered, and solvent recovery, waste water then needs to carry out sewage treatment.
The regenerating active carbon of this method can generate a large amount of waste water, cause secondary pollution, increase processing cost, the energy that steam desorption generates
It consumes also high；And cooled down using air to high temperature bed when its charcoal canister cold blowing, drying, there are higher bed windburns
Danger, safety be not high.
201610736390.8 are concentrated exhaust gas in such a way that single-stage runner adsorbs organic exhaust gas, after runner absorption
Handle gas discharge.The regeneration gas of runner concentration then carries out burning processing.This method only has level-one runner to exhaust gas and carries out at absorption
Reason, then discharged when exhaust gas concentration is high it is not up to standard, and because in the concentrated gas of runner volatile organic compounds concentration no more than explode
The 25% of lower limit LEL, institute are only suitable for handling low concentration gas in this way, can not handle the exhaust gas of middle and high concentration, fit
It is narrow with face.And rotary wheel regeneration gas is not recycled, but burning processing is carried out, it is less economical.
Summary of the invention
Purpose of design: avoiding the shortcoming in background technique, adsorbs the second combined with runner using activated carbon adsorption
Acetoacetic ester recovery method solves the problems, such as that background technique exists: first is that adsorption treatment is carried out only with Activated Carbon toward VOCs-Containing Exhausts,
It will appear after activated carbon adsorption certain time, concentration of emission reach predetermined value and discharge problem not up to standard, the switching of active carbon
Period is short, and in switching, the degree of saturation of active carbon is low, and active carbon utilization rate is low, and adsorption and desorption has frequently also increase accordingly molten
The recycling energy consumption of agent；Second is that come recycling design in such a way that active carbon is combined with runner absorption, if using steam to activity
Charcoal is regenerated, and can be generated a large amount of waste water, be caused secondary pollution, increase cost of sewage disposal；And steam desorption generation
It is also high to recycle energy consumption；And cooled down using air to high temperature bed when its charcoal canister cold blowing, drying, there are higher beds
Fire risk, safety are poor；Third is that carrying out Adsorption Concentration processing to organic exhaust gas only with zeolite runner, applicable surface is narrow, can only
The organic exhaust gas for handling low concentration, is discharged not up to standard if the exhaust gas for handling middle and high concentration；And rotary wheel regeneration gas is not returned
It receives, but carries out burning processing, it is less economical.
Design scheme: in order to solve the problems, such as that the above method exists and limitation, the present invention use activated carbon adsorption and turn
Wheel absorption combines, and active carbon, using second level tank is enriched with, thermal inertia gas is regenerated, regeneration gas is carried out using chilled water
Condensing recovery, rotary wheel regeneration gas return to system inlets circular treatment.The universality of VOCs treatment technique is enhanced, is improved
The available adsorption efficiency of active carbon, reduces the energy consumption of solvent recovery.
The present invention increases after activated carbon adsorption, second order activity charcoal solvent-rich, thermal inertia gas regeneration treatment exhaust gas
Runner absorption, keeps the system concentration of emission of activated carbon adsorption early period lower, reaches in activated carbon adsorption certain time, concentration of emission
After predetermined value, the exhaust gas that active carbon bed is discharged in runner continues to adsorb, and the qualified discharge time of exhaust is increased.It extends
The regenerated switching cycle of activated carbon adsorption, the adsorption saturation degree of active carbon when improving switching, while also reducing absorption, taking off
Attached frequently generated recycling energy consumption.
The present invention uses thermal inertia gas N instead in the technique that activated carbon adsorption (steam desorption), runner absorption combine2To work
Property charcoal regenerated, avoid the secondary pollution and waste water control cost that a large amount of waste water generate, make after also avoiding steam regeneration
The active carbon bed fire risk caused by air cold blowing.Solvent rich, second order activity canister are carried out in second order activity canister
N is used during regenerated2It is recycled, safe and efficient, energy conservation and environmental protection.
The present invention increases activated carbon adsorption processing, by living before single-stage zeolite runner handles organic exhaust gas
Property the discharge of charcoal bed low concentration gas adsorbed, be concentrated using runner, last qualified discharge is discharged after runner concentration
High concentration regeneration gas then returns to system entry, carries out circular treatment, avoids waste of solvent caused by regeneration gas is burnt, mention
High economic benefit.The present invention also can handle the tail gas of middle and high concentration, improve the pervasive of VOCs treatment technique
Property.
The condensing mode of regenerating active carbon gas is changed to chilled water by cooling water by the present invention, and condensation temperature is lower, reaches 10
~15 DEG C, freezing water condensation has two advantages: first is that the lower then solvent of condensation temperature goes out under similarly regeneration gas concentration
Liquid measure is bigger；Second is that primary activity charcoal regeneration desorption, second order activity charcoal absorption when, the adsorption effect of second order activity charcoal more preferably,
Solvent adsorption is more thorough, and the regeneration residual rate of primary activity charcoal absorber is lower, extends the qualified discharge time of exhaust gas absorption,
Simultaneously but also the absorption utilization rate of active carbon is higher.
Term is explained:
Exhaust gas absorption: absorption of the adsorption tanks to organic exhaust gas；
Regeneration desorption: to the absorber absorption heating prolapse solvent of saturation, the regeneration of absorber is completed, while being desorbed out highly concentrated
Degree exhaust gas, which enters in another adsorption tanks, to be adsorbed；
Second adsorption: it regenerates the high-concentration organic waste gas come and is adsorbed in another adsorption tanks；
Desorption condensing recovery: carrying out heating desorption to the adsorption tanks that second adsorption is completed, and the organic gas for being desorbed out passes through
Condensing recovery.With the reduction of solvent strength in desorption gas, when the concentration of exhaust gas is lower than concentration required for liquefying, desorption condensation
Complete；
Adsorption saturation: it in adsorption process, is inhaled when absorber outlet, organic exhaust gas concentration is greater than the content of a certain setting value
Attached saturation.
Runner absorption: after adsorption tanks absorption reaches saturation, absorber outlet organic exhaust gas enters runner and is adsorbed.
Rotary wheel regeneration: the solvent reclamation adsorbed on runner is come out using hot-air, completes the regeneration of molecular sieve.
Detailed description of the invention
Fig. 1, which is active carbon, to be combined with runner absorption and removes ethyl acetate process flow chart.Each label is expressed as follows in figure: valve
1 active carbon adsorption tank A of door once enters the wind valve；2 active carbon adsorption tank A of valve desorption air inlet valve；3 active carbon adsorption tank of valve
Valve for air exhaust of A；Valve for air exhaust is desorbed in 4 active carbon adsorption tank A of valve；5 active carbon adsorption tank B of valve once enters the wind valve；
6 active carbon adsorption tank B of valve desorption air inlet valve；Valve valve for air exhaust of 7 active carbon adsorption tank B；8 active carbon adsorption of valve
Valve for air exhaust is desorbed in tank B；9 active carbon adsorption tank C secondary air valve of valve；Air inlet valve is desorbed in 10 active carbon adsorption tank C of valve
Door；11 activated carbon of valve is desorbed tank C and valve for air exhaust is desorbed；Tank C secondary exhausting valve is desorbed in 12 activated carbon of valve；13 activity of valve
Carbon adsorption tank A nitrogen air intake valve；14 active carbon adsorption tank B nitrogen air intake valve of valve；15 active carbon adsorption tank C nitrogen of valve
Air intake valve；Bypass cock valve is desorbed in valve 16.
Specific embodiment
Embodiment 1: referring to attached drawing 1.A kind of ethyl acetate recycling system combined using activated carbon adsorption with runner absorption
System, including forecooler, main air blower, active carbon adsorption tank A, active carbon adsorption tank B, active carbon adsorption tank C, filter, desorption are cold
Blower, nitrogen is desorbed in condenser, level-one desorption blower, runner absorber, level-one desorption heat exchanger, runner desorption heat exchanger, second level
Tank.
The pre-cooling of organic exhaust gas: house exhaust enters in forecooler with the organic exhaust gas by rotary wheel regeneration circulation, is inhaled
Attached pre-cooling drops to the temperature of organic exhaust gas between 20~30 DEG C.
The absorption of organic exhaust gas: the organic exhaust gas to come through blower conveying enters in active carbon adsorption device A, carries out exhaust gas suction
Attached, the exhaust gas after absorption is filtered, and filtered gas enters runner absorber and adsorbed, and detects heel row up to standard
It puts.
The desorption of absorber: when detecting that outlet of rotary wheel concentration reaches setting value.Active carbon adsorption device A first is closed to enter the wind
Valve 1 and third valve for air exhaust 3 open active carbon adsorption device A second and enter the wind valve 2 and the 4th valve for air exhaust 4.Open activated carbon
Absorber B the 5th enters the wind valve 5 and the 7th valve for air exhaust 7 carries out absorber B and once adsorbs, and gas enters after filtering after absorption
Runner is adsorbed again, adsorbs rear discharge up to standard.Oxygen concentration in active carbon adsorption device A is controlled simultaneously, certainly when being higher than 1%
Dynamic Open valve 13.
The second adsorption of absorber: active carbon adsorption device A carry out heating desorption while open desorption bypass cock valve 16,
Active carbon adsorption tank C secondary air valve 9, active carbon adsorption tank C desorption air inlet valve 10, carry out two by active carbon adsorption device C
Grade absorption, is enriched with solvent.
The second air inlet of active carbon adsorption tank A desorption valve 2, active carbon adsorption tank A third valve for air exhaust 3 are opened and are carried out
The cold desorption of absorber A, until absorber A temperature drops to 20~60 DEG C.
Active carbon adsorption device A active carbon adsorption tank A desorption the second air inlet valve 2, third valve for air exhaust 3 are closed, opens and lives
Property carbon adsorption tank A once enter the wind valve 1, active carbon adsorption tank A desorption valve for air exhaust 4.Into the absorption of active carbon adsorption device A.
Active carbon adsorption device B activity carbon adsorption tank B desorption air inlet valve 6, active carbon adsorption tank B desorption valve for air exhaust 8 are opened simultaneously, together
Shi Kaiqi active carbon adsorption device B nitrogen air intake valve 14, into the thermal desorption of active carbon adsorption device B.
After active carbon adsorption device B completes thermal desorption, active carbon adsorption device B activity carbon adsorption tank B desorption air inlet valve is closed
6, valve for air exhaust 8 is desorbed in active carbon adsorption tank B.It opens active carbon adsorption tank B and once enters the wind valve 5 and active carbon adsorption tank B mono-
Secondary valve for air exhaust 7 carries out the cold desorption of active carbon adsorption device B.Until active carbon adsorption device B temperature drops to 20~60 DEG C.
It is de- to open active carbon adsorption device C desorption air intake valve 10, activated carbon desorption tank C secondary exhausting valve 12 and activated carbon
Attached tank C secondary exhausting valve 16, closes active carbon adsorption tank C secondary air valve 9 and tank C secondary exhausting valve is desorbed in activated carbon
12.The thermal desorption for carrying out active carbon adsorption device B, the organic exhaust gas for being desorbed out is by condensation discharge system.
Close active carbon adsorption device C active carbon adsorption tank C desorption air inlet valve 10, tank C secondary exhausting valve is desorbed in activated carbon
Tank C secondary exhausting valve 16 is desorbed in door 12 and activated carbon, opens active carbon adsorption tank C secondary air valve 9 and activated carbon desorption
Tank C secondary exhausting valve 12.Carry out the cold desorption of active carbon adsorption device C.
So adsorption and desorption and condensing recovery process of the circulation to system progress organic exhaust gas.
Embodiment 2: it on the basis of embodiment 1, is returned using activated carbon adsorption with the ethyl acetate that runner absorption combines
Receiving method includes following step:
Step 1: carrying out precooling treatment, treated organic exhaust gas by condenser by the organic exhaust gas that workshop and runner recycle
Disengaging absorbent charcoal adsorption tank A in adsorbed, the organic exhaust gas after absorption enter runner carry out Adsorption Concentration, gas up to standard into
Enter in atmosphere and discharges.
Step 2: when runner exhaust outlet concentration is more than setting value, closing and opening respective valves, so that absorber A enters
Desorption stage, adsorption tanks B enter the primary adsorption stage, and adsorption tanks C carries out secondary absorption.Runner carries out always molten in the process
The absorption and rotary wheel regeneration process of agent.
Step 3: adsorption tanks A thermal desorption mainly analyzes oxygen content in adsorption tanks A by determination of oxygen content, when higher than 1%
When, nitrogen supply system valve need to be opened, controls oxygen content below 1%.
Step 4: the cold desorption of adsorption tanks A, tank A layer of charcoal temperature to be adsorbed drop to setting value, unlatch and close respective valves,
Purging work is carried out, purge gas, which enters in adsorption tanks C, to be adsorbed.
Step 5: after adsorption tanks A completes desorption, carrying out adsorption operations next time, carry out the regeneration desorption of adsorption tanks C, take off
The attached organic exhaust gas come out, which enters, carries out condensing recovery in condenser, uncondensed gas, which enters in adsorption tanks B, to be adsorbed.
So circulation goes on, and completes the circular flow of system.
It is to be understood that: although above-described embodiment retouches mentality of designing of the invention detailed text of contrasting
It states, but these verbal descriptions, only the simple text of mentality of designing of the present invention is described, rather than to mentality of designing of the present invention
Limitation, any combination, increase or modification without departing from mentality of designing of the present invention falls within the protection scope of the present invention.
Claims (10)
1. a kind of adsorb the ethyl acetate recovery method combined, including PLC controller with runner using activated carbon adsorption, special
Sign is:
1) cooling of gas: house exhaust and the organic exhaust gas of rotary wheel regeneration circulation enter in forecooler, the pre-cooling adsorbed,
The temperature of organic exhaust gas is dropped between 20~30 DEG C, is transported in active carbon adsorption tank A by blower, gas passes through again after absorption
After crossing the absorption of runner absorber, the exhaust gas after absorption is filtered, and filtered gas enters runner absorber and inhaled
It is attached, reach the discharge standard of setting, is discharged into exhaust system；
2) absorber switches: when detecting that outlet of rotary wheel concentration reaches setting value, active carbon adsorption is closed in PLC controller instruction
The first air inlet valve 1 outlet of device A and third valve for air exhaust 3 open the second air inlet valve 2 and the 4th of active carbon adsorption device A
Valve for air exhaust 4, the 5th air inlet valve 5 and the 7th valve for air exhaust 7 for opening active carbon adsorption device B carry out absorber B and once adsorb,
Gas enters runner after filtering and is adsorbed again after absorption, adsorbs rear discharge up to standard, while controlling in active carbon adsorption device A
Oxygen concentration, when being higher than 1%, PLC controller instructs the nitrogen air intake valve 13 of active carbon adsorption tank A to automatically turn on, activated carbon
While absorber A carries out heating desorption, desorption bypass cock valve 16, the active carbon adsorption tank C of active carbon adsorption tank C are opened
Secondary air valve 9 and active carbon adsorption tank C desorption air inlet valve 10, carry out secondary absorption by active carbon adsorption device C, to solvent
It is enriched with；
3) fire-retardant gas is replaced: active carbon adsorption tank A is passed through fire-retardant gas and is replaced, and PLC controller is supervised according to sensor
When the oxygen content measured is lower than 1%, instruction active carbon adsorption tank A starts regeneration desorption；
4) regeneration desorption and second adsorption: by active carbon adsorption tank A, condenser, active carbon adsorption tank C, circulating fan, heater
The second adsorption circuit for forming the regeneration desorption and active carbon adsorption tank C of active carbon adsorption tank A, removes from active carbon adsorption tank A
Organic gas after condenser cools down enter active carbon adsorption tank C carry out second adsorption；
5) adsorption tanks A cools down: after the completion of active carbon adsorption tank A desorption, active carbon adsorption tank A, condenser, circulating fan group are survived
The cooling circuit of property carbon adsorption device A, recyclegas cool down to active carbon adsorption tank A；
6) heating desorption solvent condensing recovery: after active carbon adsorption tank A cools down, the air displacement in active carbon adsorption tank C
For fire-retardant gas, desorption condensing circuit is formed by active carbon adsorption tank C, condenser, circulating fan, heater, high concentration is organic
Gas is cooled to 10~15 DEG C by chilled water, carries out second level tank desorption and solvent recovery；
7) active carbon adsorption tank C is cooling: after active carbon adsorption tank C completes desorption, by active carbon adsorption tank C, condenser, circulated air
The cooling circuit of the Viability carbon adsorption tank C of unit, cools down active carbon adsorption device C；
Hereafter active carbon adsorption tank A cuts adsorption process by valve, and activated adoption tank B cuts desorption process by valve, walked
Rapid 2-7, so circulation carry out solvent recovery process.
2. according to claim 1 adsorb the ethyl acetate recovery method combined with runner using activated carbon adsorption,
Be characterized in: tail gas air inlet air quantity is in 10000~60000m3Between/h.
3. according to claim 1 adsorb the ethyl acetate recovery method combined with runner using activated carbon adsorption,
It is characterized in: 30~50 DEG C of organic exhaust gas temperature, 2000~20000mg/m of inlet gas concentration3。
4. according to claim 1 adsorb the ethyl acetate recovery method combined with runner using activated carbon adsorption,
Be characterized in: runner discharge gas is monitored by VOC gas on-line computing model.
5. according to claim 1 adsorb the ethyl acetate recovery method combined with runner using activated carbon adsorption,
Be characterized in: adsorption tanks regenerative process carries out under nitrogen protection, and adsorption tanks oxygen is monitored online by oxygen content on-line computing model
Concentration.
6. according to claim 1 adsorb the ethyl acetate recovery method combined with runner using activated carbon adsorption,
Be characterized in: regeneration desorption absorber temperature is between 120~180 DEG C.
7. according to claim 1 adsorb the ethyl acetate recovery method combined with runner using activated carbon adsorption,
Be characterized in: rotary wheel regeneration temperature is between 150~220 DEG C.
8. according to claim 1 adsorb the ethyl acetate recovery method combined with runner using activated carbon adsorption,
Be characterized in: the organic solvent being adsorbed in regeneration runner, concentrating regenerative gas concentration is the 5 of inlet concentration after the heat treatment of renewing zone
~10 times.
9. according to claim 1 adsorb the ethyl acetate recovery method combined with runner using activated carbon adsorption,
Be characterized in: the condensation of regenerating active carbon gas is carried out using chilled water, and condensation temperature is between 10~15 DEG C.
10. according to claim 1 adsorb the ethyl acetate recovery method combined with runner using activated carbon adsorption,
Be characterized in: active carbon adsorption device A second enters the wind valve 2, third valve for air exhaust 3 is opened and carries out the cold desorption of absorber A, until absorption
Device A temperature drops to 20~60 DEG C.
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| CN201811545556.3A CN109731433B (en) | 2018-12-18 | 2018-12-18 | Ethyl acetate recovery method combining activated carbon adsorption and rotary wheel adsorption |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110385008A (en) * | 2019-05-23 | 2019-10-29 | 深圳市智盾环保科技有限公司 | Vapor for handling the waste active carbon containing VOCs concentrates desorption system |
| CN111318128A (en) * | 2020-03-03 | 2020-06-23 | 青岛华世洁环保科技有限公司 | Adsorption recovery system for nitrogen regeneration and adsorption recovery method thereof |
| CN116603350A (en) * | 2023-07-14 | 2023-08-18 | 北京环都环保科技有限公司 | Waste gas recovery heat energy recycling system and method |
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Address after: 310026 No. 2088, Keji Avenue, Qingshanhu street, Lin'an District, Hangzhou City, Zhejiang Province Patentee after: Hangzhou Jierui Intelligent Equipment Co.,Ltd. Address before: 310026 No. 2088, Keji Avenue, Qingshanhu street, Lin'an District, Hangzhou City, Zhejiang Province Patentee before: HANGZHOU DRY AIR TREATMENT EQUIPMENT Co.,Ltd. |
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Denomination of invention: The recovery method of ethyl acetate using a combination of activated carbon adsorption and rotary adsorption Granted publication date: 20211210 Pledgee: Hangzhou High-tech Financing Guarantee Co.,Ltd. Pledgor: Hangzhou Jierui Intelligent Equipment Co.,Ltd. Registration number: Y2024980003748 |