CN106540508A - Reclaim the device and method of volatility organic chloride gas - Google Patents
Reclaim the device and method of volatility organic chloride gas Download PDFInfo
- Publication number
- CN106540508A CN106540508A CN201611223769.5A CN201611223769A CN106540508A CN 106540508 A CN106540508 A CN 106540508A CN 201611223769 A CN201611223769 A CN 201611223769A CN 106540508 A CN106540508 A CN 106540508A
- Authority
- CN
- China
- Prior art keywords
- adsorption tower
- condenser
- organic chloride
- chloride gas
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
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
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
- B01D53/0438—Cooling or heating systems
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0454—Controlling adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/206—Organic halogen compounds
- B01D2257/2064—Chlorine
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)
Abstract
The invention discloses reclaiming the device and method of volatility organic chloride gas.The device for reclaiming volatility organic chloride gas of the present invention, it is characterised in that include：One or more adsorption towers, in the adsorption tower, device has adsorbent resin；Heater, the heater are connected with all or part of adsorption tower, for hot gas or water vapour are input in the adsorption tower；First condenser, first condenser are connected with all or part of adsorption tower；After adsorbent resin adsorbent organic chlorine compound gas in the adsorption tower, heater is input into hot-air or water vapour into the adsorption tower, makes organic chloride gas of the absorption on the adsorbent resin depart from the adsorbent resin；And export being condensed into after liquid in organic chloride gas the first condenser of input.The organic chloride concentration given off after retracting device of the present invention and method are processed is less than 10mg/m3。
Description
Technical field
The present invention relates to reclaim the device and method of volatility organic chloride gas.
Background technology
Organic chloride (such as dichloromethane, chloroform, carbon tetrachloride, trichloro ethylene, tetrachloroethylene) etc. is organic molten
Agent is widely used in industries such as external coating, pharmaceutical synthesis, packages printing, adhesive, metal cleanings, is produced and is used process
In due to volatilization can be expelled directly out volatility organic chloride gas.It is well known that organic chloride has larger toxicity, have
Stimulate and anesthetic action.Suction acute poisoning person have upper respiratory tract irritation, shed tears, sialorrhea, occur therewith dizzy, headache,
Nausea, movement disorder and drunk sample symptom.Severe one occurs hepatic injury and poisoning, or even goes into a coma quickly.And organic chloride
There may also be stronger carcinogenecity, cause malignant tumor or leukemia.By volatility organochlorine compound cause it is a series of strong
Health, environmental and safety problems, cause the extensive concern of society.Additionally, after most of volatility organochlorine compound is recovered
Can reuse, directly discharge can cause the waste of resource.Therefore the research of effective recycling volatility organic chloride,
With great social meaning and economic benefit.
The mainstream technology that generally industrial organic exhaust gas are administered be absorption method, absorption process, combustion method, low temperature etc. from decomposition method,
Condensation method etc..Generally using activated carbon as adsorbent, literature research shows absorption method, and the humidity in air can have a strong impact on work
Property absorption of the charcoal to volatile organic matter (VOC), particularly nonpolar volatile organic matter molecule.And activated carbon service life
Shorter, the activated carbon scrapped not only had polluted environment as fixed-end forces but also had increased enterprise's use cost.Chinese patent CN102764559
Propose one kind and use activated carbon or carbon fiber adsorption and catalytic combustion volatile organic waste gas, then desorption-rectification-infiltration evaporation is separated
Processing scheme, although its separation accuracy is high, as which uses water vapour to be desorbed, after causing desorption, activated carbon adsorbs effect again
Rate is low, the poor processing effect to VOC.Additionally, use rectification and membrance separation recovery process efficiency low, so as to operating cost pole
Height, industrialization promotion obstacle are larger.Combustion method is to process one of widest method of organic exhaust gas, but due to organic chloride
The bioxin material of high poison is easily produced after burning, in this approach it is not recommended that applying at the place of volatility organic chloride waste gas
In reason.Low-temperature plasma decomposition method is only suitable only under the organic chloride substance environment of low concentration, for the organic chloride of high concentration
It is difficult to decompose completely, almost no effect, and it is possible to as the underpower of plasma generator causes organic waste edema caused by disorder of QI
Solution is incomplete, causes the secondary pollution of toxic and harmful.Chinese patent CN1561252A proposes a kind of compression condensation and reclaims
The scheme of oil gas, program equipment are complicated, and power consumption is high, as which can do energy resource supply using the burning of condensed oil gas
To compressor, so for the volatile organic waste gas basic feasible solution that can be burnt.But organic chloride burning can produce severe toxicity
Bioxin, and its combustion heat value is very low, and compression condensation method is infeasible in the process of volatility organic chloride waste gas.Cause
This, the characteristics of for volatility organic chloride waste gas, the processing method and system for developing a kind of high-efficiency environment friendly energy-conservation is urgently
Problem to be solved.
The content of the invention
It is an object of the present invention to overcome the deficiencies in the prior art, there is provided a kind of high recovery volatility of response rate
The device of organic chloride gas.
To realize object above, the present invention is achieved through the following technical solutions：
Reclaim the device of volatility organic chloride gas, it is characterised in that include：
One or more adsorption towers, in the adsorption tower, device has adsorbent resin；
Heater, the heater are connected with all or part of adsorption tower, for by hot gas or water vapour
It is input in the adsorption tower；
First condenser, first condenser are connected with all or part of adsorption tower；
After adsorbent resin adsorbent organic chlorine compound gas in the adsorption tower, heater is input into into the adsorption tower
Hot-air or water vapour, make organic chloride gas of the absorption on the adsorbent resin depart from the adsorbent resin；And will have
Machine chloride gas are input in the first condenser after being condensed into liquid and export.
Embodiment of the invention, also including the second condenser, second condenser and first condenser
Connection, so as to after organic chloride gas enters the first condenser condensation process, enter back into the second condenser relaying
Continuous condensation process.
Embodiments in accordance with the present invention, also including vacuum extractor, the vacuum extractor and first condenser and
One or two in second condenser is connected, for by evacuation in first condenser and/or the second condenser.
Embodiment of the invention, the adsorption tower include the first adsorption tower and the second adsorption tower, and described first inhales
Attached tower is connected with second adsorption tower, so that gas is Jing after the adsorbent resin absorption in the first adsorption tower, then is input into described the
Adsorbed by the adsorbent resin in which in two adsorption towers；First condenser is connected with second adsorption tower；Described second is cold
Condenser is connected with second adsorption tower, so that the gas Jing after the second condenser condensation process can be input into second absorption again
Continue absorption in tower.
Embodiment of the invention, the adsorption tower also include the 3rd adsorption tower；3rd adsorption tower with it is described
Second adsorption tower is connected；After the first adsorption tower adsorption saturation, gas is first described in after the second adsorption tower adsorption treatment, then enters
Enter the 3rd adsorption tower adsorption treatment；First condenser is connected with first adsorption tower and the 3rd adsorption tower
It is logical.
Embodiment of the invention, also including vacuum extractor, the vacuum extractor and the first condenser and/or
Second condenser connection, for by evacuation in first condenser and/or second condenser.
Another object of the present invention is to overcome the deficiencies in the prior art, there is provided a kind of high recovery volatilization of response rate
The method of property organic chloride gas.
To realize object above, the present invention is achieved through the following technical solutions：
The method for reclaiming organic chloride gas, it is characterised in that using aforesaid recovery volatility organic chloride gas
The device of body, including step：
A, organic chloride gas Jing adsorbent resin adsorption treatment；
B, the process of adsorbent resin desorption, make organic chloride gas of the absorption on adsorbent resin depart from the absorption tree
Fat；
In organic chloride gas input condenser after C, the disengaging adsorbent resin, liquid is condensed under vacuum conditions
Output after body is reclaimed.
Embodiment of the invention, in step A, organic chloride gas temperature is 10 DEG C to 80 DEG C.
Embodiment of the invention, in step A, organic chloride gas humidity is 0%-100%.
Embodiment of the invention, in step A, the concentration of organic chloride gas is 10-1000000mg/
m3。
Embodiment of the invention, in step A, organic chloride waste gas air quantity is 3000-1000000m3/
h。
Embodiment of the invention, in step B, temperature when desorption is processed is room temperature to 120 DEG C.
Embodiment of the invention, in step C, condensation temperature is -25 DEG C to -5 DEG C.
Embodiment of the invention, in step C, sequentially passes through condensation process twice, first time condensation temperature
For -15 DEG C to -5 DEG C；Second condensation temperature is -25 DEG C to -15 DEG C.
Embodiment of the invention, in step C, the vacuum in the condenser is not more than 2Kpa.
Beneficial effects of the present invention are as follows：1st, the present invention efficiently solves the neck such as external coating, metal cleaning, pharmaceutical synthesis
The recovery of the organic chloride waste gas that domain produces and Utilizing question, give off after the retracting device and method of the present invention are processed
Organic chloride concentration be less than 10mg/m3, reach country《Discharge standard of air pollutants》Require；2nd, it is of the invention to return
Receiving apparatus automation degree of equipment is high, and recovering effect is good, environmental protection and energy saving；3rd, adsorbent resin adsorption capacity is big, and advantages of good adsorption effect makes
Use the time long, resistance to high humidity is functional, can apply to the special environments such as high humidity, it is possible to which regeneration is used, and effectively can be reduced into
This；4th, the condensation effect of vacuum condensation is good, and organic efficiency is high, and operating cost is low.Therefore the present invention has good technological adaptability
And market application foreground.
Description of the drawings
Fig. 1 is the apparatus structure schematic diagram of the recovery volatility organic chloride gas in the present invention.
Specific embodiment
The present invention is described in detail with reference to embodiment and accompanying drawing.
Adsorbent resin is a kind of macromolecular compound of synthetic, has larger specific surface area, loose structure and suitable
Pore size distribution$, and its surface has carried out Modified with Polar Monomer, and its loose structure and surface polarity can be utilized efficiently to adsorb
Various volatile organic matter gases (VOCs), especially volatility organic chloride waste gas.Additionally, adsorbent resin does not receive environmental wet
The impact of degree, adsorption efficiency is high, through hole resistance is little, substantially reduces than granular active carbon vapour lock so as to more suitable for fluid bed.By
The inorganic matters such as metal are not contained in which, chemical stability is good, will not react with organic chloride, produce unknown poisonous and harmful
Material.Additionally, adsorbent resin high mechanical strength, in use, itself will not produce dust, the problems such as cause hydraulic performance decline.And it is active
It is inevitable that charcoal produces dust in use, and dust and water etc. can produce shadow to the performance and VOCs stability of activated carbon
Ring, even result in spontaneous combustion and blast.
Vacuum condensation is a kind of high efficiency method for industrially carrying out rectification and purification organic solvent, but in volatility organic waste
Gas yet there are no utilization.Here adsorbent resin system and vacuum condensing system are organically combined by we, are defined a set of effective
The system for recycling volatility organic chloride waste gas.
The present invention technology design be：Using adsorbent resin as adsorbent, active adsorption organic chloride gas, this set
System includes three adsorption towers, and wherein organic chloride waste gas is adsorbed into the first adsorption tower through air inlet；From first
After the primary adsorption discharged in adsorption tower is processed, volatility organic chloride is adsorbed into the second adsorption tower, carries out depth two
Level absorption, it is ensured that the tail gas of discharge reaches National Environmental standard；While wherein first, second adsorption tower is adsorbed,
The 3rd adsorption tower for reaching saturated adsorption capacity carries out desorption and regeneration, and circulation absorption desorption, reaches and utilize to greatest extent successively
The effect of adsorbent resin.Desorption is mainly carried out by hot-air or water vapour are input under vacuum condition, and what is be desorbed has
Machine chloride gas form liquid through vacuum condensation and flow in reservoir, and centralized recovery is utilized.The uncooled tail gas for getting off is led
Enter to adsorption tower circular treatment, prevent exceeded gas is discharged in air.
The device of the recovery volatility organic chloride gas being illustrated in figure 1 in the present invention.Which includes the first adsorption tower
101st, the second adsorption tower 102 and the 3rd adsorption tower 103, heater 110, the first condenser 120, the second condenser 130 and take out
Vacuum equipment 140.It is respectively arranged with adsorbent resin in first adsorption tower 101, the second adsorption tower 102 and the 3rd adsorption tower 103 (in figure not
Illustrate).First adsorption tower 101, the second adsorption tower 102 and the 3rd adsorption tower 103 can be serial or parallel connection, or series connection
With the mode of parallel combination.First adsorption tower 101, the second adsorption tower 102 and the 3rd adsorption tower 103 can be fixed beds, mobile
One or more combination in bed and fluid bed, preferably fluid bed.Organic chloride gas is inhaled into the first adsorption tower
Attached, wherein adsorbent is adsorbent resin；After the primary adsorption discharged from the first adsorption tower is processed, gas enters the second adsorption tower
Adsorbed, carried out depth secondary absorption.What the adsorption treatment switching of adsorption tower was controlled using programmable logic controller (PLC) (PLC)
Two-way valve or three-way valve.Organic chloride gas air quantity of the present invention is 3000-1000000m3The preferred 3000- of/h
100000m3/h；Humidity is 0%-100%, preferably 30%-90%；Concentration is 10-1000000mg/m3, preferred 100-
5000mg/m3；Temperature is 10 DEG C to 80 DEG C, preferably 20 DEG C to 40 DEG C.
The heater 110 is connected with all or part of adsorption tower, and the desorption process switching of adsorption tower is using programmable
Two-way valve or three-way valve that logic controller (PLC) is controlled.For hot gas or water vapour are input in the adsorption tower.As schemed
In shown example, heater 110 is connected with the first adsorption tower 101, the second adsorption tower 102 and the 3rd adsorption tower 103, can
Hot-air or water vapour are input into into first adsorption tower 101, the second adsorption tower 102 and the 3rd adsorption tower 103, make absorption exist
Organic chloride gas on adsorbent resin departs from adsorbent resin.Adsorbed volatility is promoted by hot-air or water vapour
Organic chloride gas is desorbed from adsorbent resin, and desorption temperature is 25 DEG C to 120 DEG C of room temperature.Desorption temperature is according to process
The boiling point of organic chloride determine that lower boiling organic chloride gas selects lower temperature desorption, high boiling organochlorine
Compound gas selects higher temperatures desorption.For example：Dichloromethane boiling point, 39.8 degrees Celsius, it is possible to select 40 degrees Celsius to be desorbed, three
Vinyl chloride, boiling point, 86.7 degrees Celsius, it is possible to select 100 degrees Celsius to be desorbed.Gas flow during desorption is into absorption
The 0.5%-2% of gas air quantity in tower.For example：It is 5 ten thousand steres/hour into the gas air quantity in adsorption tower, then desorption
Air quantity just be 250-1000 cube m/h.
First condenser 120 is connected with all or part of adsorption tower, and the organic chloride gas for being desorbed is cold
Coagulate and export for liquid.In example as depicted, the first condenser 120 and the first adsorption tower 101, the second adsorption tower 102 and
3rd adsorption tower 103 is connected.The organic chloride of desorption in first adsorption tower 101, the second adsorption tower 102 and the 3rd adsorption tower 103
Liquid is condensed in the first condenser of thing gas input 120.
Second condenser 130 is connected with first condenser 120；Organic chloride gas is cold into described first
After 120 condensation process of condenser, in entering back into second condenser 130, continue condensation process.Condensation temperature is -25 DEG C extremely -5
℃.Preferably in the first condenser 120 Jing after-15 DEG C to-5 DEG C condensation process, then in the second condensers of Jing 130-25 DEG C to-
15 DEG C of condensation process.Second condenser 130 is also connected with the second adsorption tower 102.It is uncooled Jing after the process of the second condenser 130
Gas, if monitoring is not up to organic chloride concentration and is less than 10mg/m3, then be input in the second adsorption tower 102 and further adsorb
Discharge after process.
Vacuum extractor 140 is connected with first condenser 120 and the second condenser 130, for cold by described first
Evacuation in condenser 120 and the second condenser 130, make in the first condenser 120 and the second condenser 130 vacuum be 2kPa with
Under.Vacuum extractor 140 is vacuum pump.Second condenser 130 is not provided with such as, then vacuum extractor 140 and the first condenser 120
Connection.Fluid reservoir 150 is provided with below first condenser 120, the second condenser 130.The first condensers of Jing 120 and the second condensation
Storage in the liquid organic chloride input fluid reservoir 150 that the condensation of device 130 is reclaimed.
Device to protect adsorption tower, the recovery volatility organic chloride gas in the present invention can also arrange filter
160, the particulate matter in organic chloride gas is removed, the pollution adsorbent resin such as dust therein or Oil Paint Slag is prevented, is caused tree
The space of fat absorption is blocked, and adsorption efficiency declines.
In the present invention, desorption is processed and vacuum condensation is processed and organically combined, and vacuum condensation process is divided into two grades, the first condensation
Device provides primary condensation process, and which is connected on adsorption tower, and vacuum pump keeps whole system vacuum environment.It is all to evaporate
Organic chloride gas is condensed to form liquid solvent within the condenser.As system keeps high vacuum environment, organochlorine
The boiling point of compound gas is reduced, and can be desorbed quickly at a lower temperature, is formed the organic gas of high concentration, is passed through
Primary condensation process, is effectively ensured the organic chloride being desorbed and is condensed into liquid immediately, be recovered into reservoir.
Later stage, system are especially desorbed into liquid by total condensation for the organic chloride gas that ensures to be desorbed
When middle organic chloride gas concentration is reduced, it is difficult to be condensed into liquid in the first condenser.The present invention is in the first condenser
120 rear ends are connected with a set of second condenser 130, and condensation temperature is reduced to -25 DEG C to -15 DEG C, so that in the first condenser
The 120 uncooled low concentration organic chloride gases for getting off reach real total condensation in this technical process by effectively condensing
Effect.Finally, in 130 tail end of the second condenser and three adsorption towers one of adsorption tower is connected, and adsorbs a small amount of tail gas,
Ensure that final waste gas discharge is up to standard.
Using the method in the present invention, a process difficult problem for organic chloride waste gas is efficiently solved, is significantly improved organic
The efficiency and effect of chloride waste gas process, can apply to the various organochlorines of Wind Volume, low concentration or high concentration, high humility
Compound exhaust environment.Simultaneously because adsorbent resin long service life, adsorption efficiency height, greatly reduce use cost.Further
The organic chloride solvent of recovery, if less demanding, directly can reuse, if had high demands, can carry through rectification
After pure, recycling greatlys save the cost of material of enterprise, and is conducive to environmental conservation.
By taking standard paint spray booth workshop as an example, the spatial volume in workshop is 2500 cubic metres to embodiment 1-3.
Embodiment 1
683 liters of adsorbent resiies (commercially available) are seated in adsorption tower, the adsorption tower uses design of Fluidized bed, three adsorption towers
All loaded resins in the same way.To be 850mg/m containing trichloro ethylene concentration3, the waste gas of humidity 40% is first by hole
The stage high-effective filter of 200 mesh of footpath, the Oil Paint Slag gone in removing exhaust gas or dust granule.EGT is 30 degrees Celsius, should
Waste gas in the presence of blower fan with 50,000 cubes ms/h of air quantity by the first adsorption tower 101 carry out primary adsorption, second
Adsorption tower 102 carries out secondary absorption, the tail gas concentration for monitoring the outlet of the second adsorption tower 102 using PID, as a result shows exhaust emissions
Concentration is 6mg/m3. less than national standard, after continuous adsorption treatment 4h, the first adsorption tower 101 reaches saturated adsorption capacity.Use
PLC controls the first adsorption tower 101 and is switched to desorption mode, and the second adsorption tower 102 is used as primary adsorption tower, the 3rd adsorption tower 103
As secondary absorption tower.The adsorbent resin of the saturated adsorption capacity desorption and regeneration in the first adsorption tower 101 is reached, desorption is using warm
Air, 100 degrees Celsius of temperature, the air quantity of desorption is 1000m3/ h, while desorption, vacuum pump and the first adsorption tower 101 it
Between the first condenser 120 trichloro ethylene being desorbed is condensed into into liquid.Vacuum in first condenser 120 exists
2kPa, condensation temperature are -10 DEG C, condense through primary vacuum, can reclaim 52.3% trichloro ethylene.By uncooled gas
Continue to be passed in the second condenser 130, in the second condenser 130, in 2kPa, condensation temperature is -20 DEG C to vacuum, Jing Guo
Two condensers, 130 vacuum condensation, can reclaim 47.2% trichloro ethylene, and overall recovery reaches 99.5%, remaining next tail gas
The 3rd adsorption tower 103 (secondary absorption tower) is returned to, circulation absorption vacuum condensation is reclaimed, until up to standard.
Embodiment 2
683 liters of adsorbent resiies (commercially available) are seated in adsorption tower, the adsorption tower uses design of Fluidized bed, three adsorption towers
All loaded resins in the same way.Will be containing trichloro ethylene concentration 850mg/m3, the waste gas of humidity 80% is first by aperture
The stage high-effective filter of 200 mesh, the Oil Paint Slag gone in removing exhaust gas or dust granule.EGT is 25 degrees Celsius, and this gives up
Gas carries out primary adsorption, second suction by the first adsorption tower 101 with 40,000 cubes ms/h of air quantity in the presence of blower fan
Attached tower 102 carries out secondary absorption, the tail gas concentration for monitoring the outlet of the second adsorption tower 102 using PID, as a result shows that exhaust emissions is dense
Spend for 7.1mg/m3. less than national standard, after continuous adsorption treatment 4h, the first adsorption tower 101 reaches saturated adsorption capacity.Use
First adsorption tower 101 is switched to desorption mode by PLC controls, and the second adsorption tower 102 is used as primary adsorption tower, the 3rd adsorption tower
103 used as secondary absorption tower.Reach the adsorbent resin of the saturated adsorption capacity desorption and regeneration in the first adsorption tower 101.Desorption makes
With hot-air, 100 degrees Celsius of temperature, the air quantity of desorption is 1000m3/ h, while desorption, in vacuum extractor 140 and first
The trichloro ethylene being desorbed is condensed into liquid by the first condenser 120 between adsorption tower 101, in the first condenser 120
In 1.5kPa, condensation temperature is -15 DEG C to vacuum, condenses through primary vacuum, can reclaim 52.1% trichloro ethylene, will not
The gas of condensation continues to be passed into the second condenser 130, and in the second condenser 130, in 2kPa, condensation temperature is -25 to vacuum
DEG C, through second vacuum condensation, 47.3% trichloro ethylene can be reclaimed, overall recovery reaches 99.4%, remaining next tail
Gas returns to the 3rd adsorption tower 103 (secondary absorption tower), and circulation absorption vacuum condensation is reclaimed.As a result it is visible in high humidity environment
Under, adsorbent resin is almost uninfluenced.
Embodiment 3
683 liters of adsorbent resiies (commercially available) are seated in adsorption tower, the adsorption tower uses design of Fluidized bed, three adsorption towers
All loaded resins in the same way.To be 2000mg/m containing tce concentration3, the organic exhaust gas of humidity 40% are first
By the stage high-effective filter of 200 mesh of aperture, the Oil Paint Slag gone in removing exhaust gas or dust granule.EGT is 35 Celsius
Degree, the waste gas carry out one-level suction by the first adsorption tower 101 with 30,000 cubes ms/h of air quantity in the presence of blower fan
It is attached), the second adsorption tower 102 carry out secondary absorption), using PID monitor adsorption tower two outlet tail gas concentration, as a result show tail gas
Concentration of emission is that 7.6mg/m3. is less than national standard, and after continuous adsorption treatment 4h, the first adsorption tower 101 reaches saturation absorption to be held
Amount.The first adsorption tower 101 is controlled using PLC and is switched to desorption mode, the second adsorption tower 102 as primary adsorption tower, the 3rd
Adsorption tower 103 is used as secondary absorption tower.The adsorbent resin of the saturated adsorption capacity desorption and regeneration in the first adsorption tower 101 is reached,
It is desorbed and uses hot-air, 120 degrees Celsius of temperature, the air quantity of desorption is 1000m3/ h, desorption time 30min, while desorption,
The tetrachloroethylene being desorbed is condensed into liquid by the first condenser between vacuum extractor 140 and the first adsorption tower 101
Body, in 1kPa, condensation temperature is -10 DEG C to the vacuum in the first condenser 120, condenses through primary vacuum, can reclaim
53.1% tetrachloroethylene, uncooled gas is continued to be passed in the second condenser 130, vacuum in the second condenser 130
Degree is -15 DEG C in 1.5kPa, condensation temperature, through 130 vacuum condensation of the second condenser, can reclaim 46.5% four chloroethenes
Alkene, overall recovery reach 99.6%, and remaining next tail gas returns to the 3rd adsorption tower 103 (secondary absorption tower), and circulation absorption is true
Air cooling is solidifying to be reclaimed.As a result it is visible for tetrachloroethylene, it is as a result consistent with trichloro ethylene, have good recovering effect.
Embodiment 4
683 liters of adsorbent resiies (commercially available) are seated in adsorption tower, the adsorption tower uses design of Fluidized bed, three adsorption towers
All loaded resins in the same way.To be 850mg/m containing trichloro ethylene concentration3, the gas of humidity 20% is first by hole
The stage high-effective filter of 200 mesh of footpath, the Oil Paint Slag gone in removing exhaust gas or dust granule.EGT is 15 degrees Celsius, should
Waste gas in the presence of blower fan with 3,000 cubes ms/h of air quantity by the first adsorption tower 101 carry out primary adsorption, second
Adsorption tower 102 carries out secondary absorption, the tail gas concentration for monitoring the outlet of the second adsorption tower 102 using PID, as a result shows exhaust emissions
Concentration is 5mg/m3. less than national standard, after continuous adsorption treatment 5h, the first adsorption tower 101 reaches saturated adsorption capacity.Use
PLC controls the first adsorption tower 101 and is switched to desorption mode, and the second adsorption tower 102 is used as primary adsorption tower, the 3rd adsorption tower 103
As secondary absorption tower.The adsorbent resin of the saturated adsorption capacity desorption and regeneration in the first adsorption tower 101 is reached, desorption is using warm
Air, 95 degrees Celsius of temperature, the air quantity of desorption is 20m3/ h, while desorption, between vacuum pump and the first adsorption tower 101
The trichloro ethylene being desorbed is condensed into liquid by the first condenser 120.Vacuum in first condenser 120 is in 2kPa, cold
Solidifying temperature is -6 DEG C, condenses through primary vacuum, can reclaim 45.3% trichloro ethylene.Uncooled gas is continued to be passed through
To in the second condenser 130, in the second condenser 130, in 1.5kPa, condensation temperature is -25 DEG C to vacuum, through the second condensation
130 vacuum condensation of device, can reclaim 53.2% trichloro ethylene, and overall recovery reaches 98.5%, and remaining next tail gas is returned to
3rd adsorption tower 103 (secondary absorption tower), circulation absorption vacuum condensation are reclaimed, until up to standard.
Embodiment 5
683 liters of adsorbent resiies (commercially available) are seated in adsorption tower, the adsorption tower uses design of Fluidized bed, three adsorption towers
All loaded resins in the same way.Will be containing trichloro ethylene concentration 850mg/m3, the waste gas of humidity 55% is first by aperture
The stage high-effective filter of 200 mesh, the Oil Paint Slag gone in removing exhaust gas or dust granule.EGT is 40 DEG C of waste gas in wind
Primary adsorption, the second adsorption tower are carried out by the first adsorption tower 101 with 90,000 cubes ms/h of air quantity in the presence of machine
102 carry out secondary absorption, the tail gas concentration for monitoring the outlet of the second adsorption tower 102 using PID, as a result show that exhaust emissions concentration is
6.1mg/m3. less than national standard, after continuous adsorption treatment 4h, the first adsorption tower 101 reaches saturated adsorption capacity.Using PLC
First adsorption tower 101 is switched to desorption mode by control, and the second adsorption tower 102 is made as primary adsorption tower, the 3rd adsorption tower 103
For secondary absorption tower.Reach the adsorbent resin of the saturated adsorption capacity desorption and regeneration in the first adsorption tower 101.Desorption is empty using heat
Gas, 98 degrees Celsius of temperature, the air quantity of desorption is 450m3/ h, while desorption, in vacuum extractor 140 and the first adsorption tower 101
Between the first condenser 120 trichloro ethylene being desorbed is condensed into into liquid, the vacuum in the first condenser 120 exists
1kPa, condensation temperature are -15 DEG C, condense through primary vacuum, can reclaim 50.1% trichloro ethylene, by uncooled gas
Continue to be passed into the second condenser 130, in the second condenser 130, in 2kPa, condensation temperature is -23 DEG C to vacuum, through second
Secondary vacuum condensation, can reclaim 48.1% trichloro ethylene, and overall recovery reaches 98.2%, and remaining next tail gas returns to the 3rd
Adsorption tower 103 (secondary absorption tower), circulation absorption vacuum condensation are reclaimed.As a result it is visible under high humidity environment, adsorbent resin is several
It is uninfluenced.
Embodiment 6
683 liters of adsorbent resiies (commercially available) are seated in adsorption tower, the adsorption tower uses design of Fluidized bed, three adsorption towers
All loaded resins in the same way.To be 2000mg/m containing tce concentration3, the organic exhaust gas of humidity 95% are first
By the stage high-effective filter of 200 mesh of aperture, the Oil Paint Slag gone in removing exhaust gas or dust granule.EGT should for 75 DEG C
Waste gas carries out primary adsorption by the first adsorption tower 101 with 10,000 cubes ms/h of air quantity in the presence of blower fan),
Two adsorption towers 102 carry out secondary absorption), as a result the tail gas concentration for monitoring the outlet of adsorption tower two using PID show that exhaust emissions is dense
It is that 7.4mg/m3. is less than national standard to spend, and after continuous adsorption treatment 4h, the first adsorption tower 101 reaches saturated adsorption capacity.Use
PLC controls the first adsorption tower 101 and is switched to desorption mode, and the second adsorption tower 102 is used as primary adsorption tower, the 3rd adsorption tower
103 used as secondary absorption tower.The adsorbent resin of the saturated adsorption capacity desorption and regeneration in the first adsorption tower 101 is reached, desorption makes
With hot-air, 120 degrees Celsius of temperature, the air quantity of desorption is 150m3/ h, desorption time 30min, while desorption, in evacuation
The tetrachloroethylene being desorbed is condensed into liquid by the first condenser between device 140 and the first adsorption tower 101, and first
In 2kPa, condensation temperature is -9 DEG C to vacuum in condenser 120, condenses through primary vacuum, can reclaim the four of 50.4%
Vinyl chloride, uncooled gas is continued to be passed in the second condenser 130, in the second condenser 130 vacuum in 0.5kPa,
Condensation temperature is -16 DEG C, through 130 vacuum condensation of the second condenser, can reclaim 45.7% tetrachloroethylene, and overall recovery reaches
To 96.1%, remaining next tail gas returns to the 3rd adsorption tower 103 (secondary absorption tower), and circulation absorption vacuum condensation is reclaimed.Knot
It is really visible for tetrachloroethylene, it is as a result consistent with trichloro ethylene, have good recovering effect.
Comparative example 1
The present invention is reclaimed into the adsorbent resin in the device of volatility organic chloride gas and is replaced by activated carbon.By 683
Rise granular active carbon (commercially available) to be seated in adsorption tower, the adsorption tower uses design of Fluidized bed, and three adsorption towers are all with same
Mode loaded resin.To be 850mg/m containing trichloro ethylene concentration3, the organic exhaust gas of humidity 40% are first by aperture 200
Purpose stage high-effective filter, the Oil Paint Slag gone in removing exhaust gas or dust granule, the waste gas in the presence of blower fan with 50,
000 cube m/h of air quantity carries out primary adsorption by the first adsorption tower 101), the second adsorption tower 102 carry out two grades suction
It is attached), the tail gas concentration of the outlet of adsorption tower two is monitored using PID, as a result show that exhaust emissions concentration is 39.8mg/m3, higher than state
Family's standard.Below standard tail gas, is recycled to the first adsorption tower 101 and continues absorption, after continuous adsorption treatment 2h, the first adsorption tower
101 reach saturated adsorption capacity.The first adsorption tower 101 is switched to into desorption mode using PLC controls, the second adsorption tower 102 is made
For primary adsorption tower, the 3rd adsorption tower 103 is used as secondary absorption tower.It is desorbed and uses hot-air, 100 degrees Celsius of temperature, desorption
Air quantity is 1000m3/ h, desorption time 2h, while desorption, first between vacuum extractor 140 and the first adsorption tower 101
The trichloro ethylene being desorbed is condensed into liquid by condenser 120, and condensation temperature is -10 DEG C, is condensed through primary vacuum, can
32.3% trichloro ethylene is reclaimed, uncooled gas is continued to be passed into senior vacuum condensing system, vacuum is in 2kPa, cold
Solidifying temperature is -20 DEG C, through senior vacuum condensation, can reclaim 26.4% tetrachloroethylene, and overall recovery reaches 58.7%, remaining
The tail gas for getting off returns to the 3rd adsorption tower 103 (secondary absorption tower), and circulation absorption vacuum condensation is reclaimed.As a result it is visible relative to
Adsorbent resin system, the adsorption efficiency of activated carbon are low, and desorption time is long, and recovering effect is poor.
Comparative example 2
The present invention is reclaimed into the adsorbent resin in the device of volatility organic chloride gas and is replaced by activated carbon.By 683
Rise granular active carbon (commercially available) to be seated in adsorption tower, the adsorption tower uses design of Fluidized bed, and three adsorption towers are all with same
Mode loaded resin.By concentration 850mg/m3, the organic exhaust gas of the trichloro ethylene of humidity 80% are first by 200 purpose three of aperture
Level high efficiency particulate air filter, the Oil Paint Slag gone in removing exhaust gas or dust granule, the waste gas in the presence of blower fan with 50,000 cube
M/h air quantity by the first adsorption tower 101 (primary adsorption), the second adsorption tower 102 (secondary absorption), monitored using PID
The tail gas concentration of the outlet of adsorption tower two, as a result shows that exhaust emissions concentration is much higher than national standard for 297.6mg/m3., does not have
Tail gas up to standard, is recycled to the first adsorption tower 101 and continues absorption, and after continuous adsorption treatment 30min, the first adsorption tower 101 reaches
Saturated adsorption capacity.Control for the first adsorption tower 101 to be switched to desorption mode using PLC, the second adsorption tower 102 is inhaled as one-level
Attached tower, the 3rd adsorption tower 103 is used as secondary absorption tower.The adsorbent resin for reaching saturated adsorption capacity is desorbed again in adsorption tower
Raw, in 2kPa, desorption uses the hot-air, 100 degrees Celsius of temperature, the air quantity of desorption to be to the vacuum of primary vacuum condenser system
1000m3/h, desorption time 2h, while desorption, the condenser between vacuum extractor 140 and the first adsorption tower 101 will be desorbed
The trichloro ethylene for getting off is condensed into liquid, and condensation temperature is -10 DEG C, condenses through primary vacuum, can reclaim the three of 12.2%
Vinyl chloride, uncooled gas is continued to be passed into senior vacuum condensing system, and in 2kPa, condensation temperature is -20 DEG C to vacuum,
Through senior vacuum condensation, 6.6% tetrachloroethylene can be reclaimed, overall recovery reaches 18.8%, and remaining next tail gas is returned
To the 3rd adsorption tower 103 (secondary absorption tower), the recovery of circulation absorption vacuum condensation.As a result absorption of the visible moisture content to activated carbon
Efficiency affects very big, almost loses adsorption effect, does not possess use value.
Comparative example 3
The vacuum extractor present invention reclaimed in the device of volatility organic chloride gas is removed.683 liters are adsorbed
Resin (commercially available) is seated in adsorption tower, and the adsorption tower uses design of Fluidized bed, three adsorption towers all to load in the same way
Resin.To be 2000mg/m containing tce concentration3, the organic exhaust gas of humidity 40% are first by 200 purpose three of aperture
Level high efficiency particulate air filter, the Oil Paint Slag gone in removing exhaust gas or dust granule, the waste gas in the presence of blower fan with 30,000 cube
M/h air quantity by the first adsorption tower 101 (primary adsorption), the second adsorption tower 102 (secondary absorption), monitored using PID
The tail gas concentration of the outlet of adsorption tower two, as a result shows that exhaust emissions concentration is 7.6mg/m3. less than national standard, at continuous absorption
After reason 4h, the first adsorption tower 101 reaches saturated adsorption capacity.The first adsorption tower 101 is controlled using PLC and is switched to desorption mode,
, used as primary adsorption tower, the 3rd adsorption tower 103 is used as secondary absorption tower for second adsorption tower 102.Reach saturated adsorption capacity
Adsorbent resin desorption and regeneration in the first adsorption tower 101, desorption use the hot-air, 120 degrees Celsius of temperature, the air quantity of desorption to be
1000m3/ h, desorption time 30min, during desorption, no vacuum extractor, under normal pressure, the first condenser is by the tetrachloro being desorbed
Ethylene is condensed into liquid, and condensation temperature is -10 DEG C, condenses through primary vacuum, can reclaim 23.5% tetrachloroethylene, will not
The gas of condensation continues to be passed in the second condenser 130, and condensation temperature is -20 DEG C, cold through 130 vacuum of the second condenser
It is solidifying, 26.7% tetrachloroethylene can be reclaimed, overall recovery reaches 50.2%, and remaining next tail gas returns to the 3rd adsorption tower
103 (secondary absorption towers), circulation absorption vacuum condensation are reclaimed.If as a result visible no vacuum extractor, the absorption effect of resin
Rate does not have impacted, and discharge gas can be up to standard, but the efficiency that condensation is reclaimed will be substantially reduced.
Beneficial effects of the present invention are as follows：1st, the present invention efficiently solves the neck such as external coating, metal cleaning, pharmaceutical synthesis
The recovery of the organic chloride waste gas that domain produces and Utilizing question, give off after the retracting device and method of the present invention are processed
Organic chloride concentration be less than 10mg/m3, reach country《Discharge standard of air pollutants》Require；2nd, it is of the invention to return
Receiving apparatus automation degree of equipment is high, and recovering effect is good, environmental protection and energy saving；3rd, adsorbent resin adsorption capacity is big, and advantages of good adsorption effect makes
Use the time long, resistance to high humidity is functional, can apply to the special environments such as high humidity, it is possible to which regeneration is used, and effectively can be reduced into
This；4th, the condensation effect of vacuum condensation is good, and organic efficiency is high, and operating cost is low.Therefore the present invention has good technological adaptability
And market application foreground.
Embodiment in the present invention is only used for that the present invention will be described, does not constitute the restriction to right,
Other replacements being substantially equal to that those skilled in that art are contemplated that, in the scope of the present invention.
Claims (15)
1. the device of volatility organic chloride gas is reclaimed, it is characterised in that included：
One or more adsorption towers, in the adsorption tower, device has adsorbent resin；
Heater, the heater are connected with all or part of adsorption tower, for hot gas or water vapour are input into
In the adsorption tower；
First condenser, first condenser are connected with all or part of adsorption tower；
After adsorbent resin adsorbent organic chlorine compound gas in the adsorption tower, heater is input into hot sky into the adsorption tower
Gas or water vapour, make organic chloride gas of the absorption on the adsorbent resin depart from the adsorbent resin；And by organochlorine
Compound gas is input in the first condenser after being condensed into liquid and exports.
2. it is according to claim 1 reclaim volatility organic chloride gas device, it is characterised in that also including second
Condenser, second condenser are connected with first condenser, so that organic chloride gas is into the described first condensation
After device condensation process, in entering back into second condenser, continue condensation process.
3. the device for reclaiming volatility organic chloride gas according to claim 2, it is characterised in that also true including taking out
Empty device, the vacuum extractor are connected with one or two in first condenser and the second condenser, for will
Evacuation in first condenser and/or the second condenser.
4. it is according to claim 2 reclaim volatility organic chloride gas device, it is characterised in that the adsorption tower
Including the first adsorption tower and the second adsorption tower, first adsorption tower is connected with second adsorption tower, so that gas Jing first
After adsorbent resin absorption in adsorption tower, then it is input in second adsorption tower by the adsorbent resin absorption in which；Described first
Condenser is connected with second adsorption tower；Second condenser is connected with second adsorption tower, so that Jing second is condensed
Gas after device condensation process can be input into again in second adsorption tower and continue absorption.
5. the device of the recovery volatility organic chloride gas according to claim 1 or 4, it is characterised in that the suction
Attached tower also includes the 3rd adsorption tower；3rd adsorption tower is connected with second adsorption tower；In the first adsorption tower adsorption saturation
Afterwards, gas after the second adsorption tower adsorption treatment, enters back into the 3rd adsorption tower adsorption treatment first described in；Described first is cold
Condenser is connected with first adsorption tower and the 3rd adsorption tower.
6. the device for reclaiming volatility organic chloride gas according to claim 2, it is characterised in that also true including taking out
Empty device, the vacuum extractor are connected with the first condenser and/or second condenser, for by first condenser
And/or evacuation in second condenser.
7. the method for reclaiming organic chloride gas, it is characterised in that usage right is required described in 1 to 6 any claim
Reclaim the device of volatility organic chloride gas, including step：
A, organic chloride gas Jing adsorbent resin adsorption treatment；
B, the process of adsorbent resin desorption, make organic chloride gas of the absorption on adsorbent resin depart from the adsorbent resin；
In organic chloride gas input condenser after C, the disengaging adsorbent resin, after being condensed into liquid under vacuum conditions
Output is reclaimed.
8. it is according to claim 7 reclaim volatility organic chloride gas method, it is characterised in that step A
In, organic chloride gas temperature is 10 DEG C to 80 DEG C.
9. it is according to claim 7 reclaim volatility organic chloride gas method, it is characterised in that step A
In, organic chloride gas humidity is 0%-100%.
10. it is according to claim 7 reclaim volatility organic chloride gas method, it is characterised in that step A
In, the concentration of organic chloride gas is 10-1000000mg/m3。
11. methods for reclaiming volatility organic chloride gas according to claim 7, it is characterised in that step A
In, organic chloride waste gas air quantity is 3000-1000000m3/h。
12. methods for reclaiming volatility organic chloride gas according to claim 7, it is characterised in that step B
In, temperature when desorption is processed is room temperature to 120 DEG C.
13. methods for reclaiming volatility organic chloride gas according to claim 7, it is characterised in that step C
In, condensation temperature is -25 DEG C to -5 DEG C.
14. methods for reclaiming volatility organic chloride gas according to claim 13, it is characterised in that the step
In C, condensation process twice is sequentially passed through, first time condensation temperature is -15 DEG C to -5 DEG C；Second condensation temperature be -25 DEG C to -
15℃。
15. methods for reclaiming volatility organic chloride gas according to claim 7, it is characterised in that step C
In, the vacuum in the condenser is not more than 2Kpa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611223769.5A CN106540508A (en) | 2016-12-27 | 2016-12-27 | Reclaim the device and method of volatility organic chloride gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611223769.5A CN106540508A (en) | 2016-12-27 | 2016-12-27 | Reclaim the device and method of volatility organic chloride gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106540508A true CN106540508A (en) | 2017-03-29 |
Family
ID=58396194
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611223769.5A Pending CN106540508A (en) | 2016-12-27 | 2016-12-27 | Reclaim the device and method of volatility organic chloride gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106540508A (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109731436A (en) * | 2019-01-21 | 2019-05-10 | 维珂瑞（北京）环境科技有限公司 | A kind of methylene chloride exhaust gas treatment method |
| CN109999616A (en) * | 2019-02-20 | 2019-07-12 | 太仓市宝马油脂设备有限公司 | A kind of tail gas absorbing system and technique in oil extraction workshop |
| CN110812876A (en) * | 2019-12-23 | 2020-02-21 | 麦德科技(无锡)有限公司 | Emission reduction system for organic solvent cleaning equipment |
| CN111359363A (en) * | 2020-02-18 | 2020-07-03 | 上海兰宝环保科技有限公司 | System for purifying chlorine-containing volatile organic waste gas |
| CN112090223A (en) * | 2020-07-22 | 2020-12-18 | 山东密友机械有限公司 | Zero-emission organic solvent recovery system |
| CN112107957A (en) * | 2019-06-19 | 2020-12-22 | 中国石油化工股份有限公司 | Butanol gas recovery device and method |
| CN112495125A (en) * | 2020-11-03 | 2021-03-16 | 杭州中环环保工程有限公司 | Dichloromethane waste gas treatment equipment and method |
| CN113069884A (en) * | 2021-04-20 | 2021-07-06 | 焦作大学 | Chemical industry workshop waste gas environmental protection filters emission equipment |
| CN113082932A (en) * | 2020-01-08 | 2021-07-09 | 江苏恒辉安防股份有限公司 | System and method for recovering and recycling tetrachloroethylene |
| CN113731116A (en) * | 2021-08-09 | 2021-12-03 | 福建省鑫森炭业股份有限公司 | A fully automatic movable integrated device for efficiently recovering organic gas and its use method |
| CN115414762A (en) * | 2022-09-06 | 2022-12-02 | 安徽东至广信农化有限公司 | Tail gas treatment method for adjacent nitrate workshop |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007197548A (en) * | 2006-01-26 | 2007-08-09 | Taiyo Nippon Sanso Corp | Method for removing siloxane in digestion gas |
| JP2008068205A (en) * | 2006-09-14 | 2008-03-27 | Syst Enji Service Kk | Method for cleaning large quantity of exhaust gas containing lean volatile hydrocarbon |
| CN103877827A (en) * | 2014-02-25 | 2014-06-25 | 浙江工业大学 | Organic waste gas adsorbing recovery device and process |
| CN104107621A (en) * | 2014-08-06 | 2014-10-22 | 南京大学 | Nitrogen purging-assisted organic exhaust gas recycling method through pressure swing adsorption of adsorbent resin |
| CN105498446A (en) * | 2016-01-08 | 2016-04-20 | 浙江大学 | Method for recycling organic matter through organic waste gas adsorption, steam desorption and fractional condensation |
| CN205360648U (en) * | 2015-11-10 | 2016-07-06 | 中山凯旋真空技术工程有限公司 | Vacuum condenser and vacuum flash evaporation system provided with the vacuum condenser |
| CN105854513A (en) * | 2016-06-08 | 2016-08-17 | 浙江奇彩环境科技股份有限公司 | Treatment method for chlorinated paraffin waste gas |
| CN205796591U (en) * | 2016-07-11 | 2016-12-14 | 成都山海油脂有限公司 | Vacuum condensation retracting device |
| CN206577554U (en) * | 2016-12-27 | 2017-10-24 | 新阳硅密（上海）半导体技术有限公司 | Reclaim the device of volatility organic chloride gas |
-
2016
- 2016-12-27 CN CN201611223769.5A patent/CN106540508A/en active Pending
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007197548A (en) * | 2006-01-26 | 2007-08-09 | Taiyo Nippon Sanso Corp | Method for removing siloxane in digestion gas |
| JP2008068205A (en) * | 2006-09-14 | 2008-03-27 | Syst Enji Service Kk | Method for cleaning large quantity of exhaust gas containing lean volatile hydrocarbon |
| CN103877827A (en) * | 2014-02-25 | 2014-06-25 | 浙江工业大学 | Organic waste gas adsorbing recovery device and process |
| CN104107621A (en) * | 2014-08-06 | 2014-10-22 | 南京大学 | Nitrogen purging-assisted organic exhaust gas recycling method through pressure swing adsorption of adsorbent resin |
| CN205360648U (en) * | 2015-11-10 | 2016-07-06 | 中山凯旋真空技术工程有限公司 | Vacuum condenser and vacuum flash evaporation system provided with the vacuum condenser |
| CN105498446A (en) * | 2016-01-08 | 2016-04-20 | 浙江大学 | Method for recycling organic matter through organic waste gas adsorption, steam desorption and fractional condensation |
| CN105854513A (en) * | 2016-06-08 | 2016-08-17 | 浙江奇彩环境科技股份有限公司 | Treatment method for chlorinated paraffin waste gas |
| CN205796591U (en) * | 2016-07-11 | 2016-12-14 | 成都山海油脂有限公司 | Vacuum condensation retracting device |
| CN206577554U (en) * | 2016-12-27 | 2017-10-24 | 新阳硅密（上海）半导体技术有限公司 | Reclaim the device of volatility organic chloride gas |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109731436A (en) * | 2019-01-21 | 2019-05-10 | 维珂瑞（北京）环境科技有限公司 | A kind of methylene chloride exhaust gas treatment method |
| CN109999616A (en) * | 2019-02-20 | 2019-07-12 | 太仓市宝马油脂设备有限公司 | A kind of tail gas absorbing system and technique in oil extraction workshop |
| CN112107957A (en) * | 2019-06-19 | 2020-12-22 | 中国石油化工股份有限公司 | Butanol gas recovery device and method |
| CN110812876A (en) * | 2019-12-23 | 2020-02-21 | 麦德科技(无锡)有限公司 | Emission reduction system for organic solvent cleaning equipment |
| CN113082932A (en) * | 2020-01-08 | 2021-07-09 | 江苏恒辉安防股份有限公司 | System and method for recovering and recycling tetrachloroethylene |
| CN111359363A (en) * | 2020-02-18 | 2020-07-03 | 上海兰宝环保科技有限公司 | System for purifying chlorine-containing volatile organic waste gas |
| CN112090223A (en) * | 2020-07-22 | 2020-12-18 | 山东密友机械有限公司 | Zero-emission organic solvent recovery system |
| CN112495125A (en) * | 2020-11-03 | 2021-03-16 | 杭州中环环保工程有限公司 | Dichloromethane waste gas treatment equipment and method |
| CN113069884A (en) * | 2021-04-20 | 2021-07-06 | 焦作大学 | Chemical industry workshop waste gas environmental protection filters emission equipment |
| CN113069884B (en) * | 2021-04-20 | 2023-03-21 | 焦作大学 | Chemical industry workshop waste gas environmental protection filters emission equipment |
| CN113731116A (en) * | 2021-08-09 | 2021-12-03 | 福建省鑫森炭业股份有限公司 | A fully automatic movable integrated device for efficiently recovering organic gas and its use method |
| CN115414762A (en) * | 2022-09-06 | 2022-12-02 | 安徽东至广信农化有限公司 | Tail gas treatment method for adjacent nitrate workshop |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106540508A (en) | Reclaim the device and method of volatility organic chloride gas | |
| CN101288820B (en) | Active carbon fiber organic gas recovery method and system using nitrogen as desorption medium | |
| CN104258688B (en) | Organic waste gas recycling system and technique | |
| CN205495288U (en) | Near zero emission's gaseous resource recovery processing device of VOCs | |
| CN103990351B (en) | A kind of purification recovery device of volatile organic waste gas | |
| CN203556260U (en) | Recovery device of easily volatile organic solvent in wastewater or waste gas | |
| CN101301558A (en) | Activated carbon fiber organic solvent recovery novel technique using nitrogen as desorption medium | |
| CN106110833A (en) | A kind of new technology processing industry VOCs waste gas | |
| CN104524929A (en) | Efficient energy-saving purification and recovery process of tail gas containing volatile organic compounds (VOCs) | |
| CN103463932B (en) | Method and device for treating and recycling organic exhaust gas with low concentration and large air volume | |
| CN102489106B (en) | Method for cycle collection of exhaust gas by adopting secondary adsorption | |
| CN104587799B (en) | Device and method for processing complex organic waste gas components and recycling resources | |
| CN110917814A (en) | Printing industry and other trades energy saving and emission reduction exhaust treatment system who discharges VOCs waste gas | |
| CN100364643C (en) | A method and device for absorbing, recovering and purifying organic matter from exhaust gas | |
| CN109731436A (en) | A kind of methylene chloride exhaust gas treatment method | |
| CN109224754A (en) | Volatile organic matter condensate recycling device and its recovery method based on macroreticular resin | |
| CN106178846B (en) | The exhaust system of ECH organic tail gas is reduced in epoxy resin production | |
| CN206577554U (en) | Reclaim the device of volatility organic chloride gas | |
| CN110227329A (en) | Waste gas treatment process in a kind of production of cyanate ester resin | |
| CN105561725A (en) | Waste water recycling device and method in VOCs waste gas recovery process | |
| CN206587550U (en) | A kind of fabric forming machine emission-control equipment | |
| CN103961997B (en) | A kind of ammonium metavanadate roaster gives off the recovery process of tail gas | |
| CN102476013A (en) | Novel organic waste gas recovery method and system | |
| CN103566702A (en) | Method for recycling gas generated in benzene lading process at wharfs | |
| CN103432862B (en) | Recovery device and method for recovering acetone waste gas by utilizing recovery device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20170329 |