CN1504252A - Process for reclaiming polymer - Google Patents
Process for reclaiming polymer Download PDFInfo
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- CN1504252A CN1504252A CNA021530297A CN02153029A CN1504252A CN 1504252 A CN1504252 A CN 1504252A CN A021530297 A CNA021530297 A CN A021530297A CN 02153029 A CN02153029 A CN 02153029A CN 1504252 A CN1504252 A CN 1504252A
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Abstract
The invention provides a polymer recovery method, wherein the polymer powder is separated and reclaimed from a part of the polymer emulsion to feed to the condenser for moisture condensation, then it is led into the straight flame heating installation for heating and re-circulation. The also provides a polymer recovery method by using small-sized condenser.
Description
Technical field
The present invention relates to from polymer emulsion, reclaim the spray drying treatment technology of polymer powder.
Technical background
From polymer emulsion, reclaiming in the method for polymer powder, adopt polymer emulsion direct spray-dired technology in hot blast.
With polymer emulsion direct technology of spraying in hot blast owing to can directly obtain dry powder from the polymer emulsion after the polymerization, so can simplify working process, the viewpoint of slave unit cost, operational management, industrial be preferred process.Spraying drying can adopt open cycle or closed circulation.
In open cycle, the heated air of dry polymer emulsion is discharged to the atmosphere by moisture eliminator after polymer emulsion reclaims polymkeric substance with the powder form.The loss that high-temperature gas is discharged to energy in the atmosphere is very big, and also troubling to the baneful influence of environment.
On the other hand, in closed circulation,, turn back to moisture eliminator again, thereby can save the fuel of supplying with well heater, reduce carrying cost by heater heats from the part of moisture eliminator expellant gas.Because the gas volume that enters in the atmosphere is few, the influence that compares environment with open cycle is also little in addition.
Also have,, in spray-drying process, must prevent dust explosion to being that the powder of the easy generation dust explosion of representative carries out the occasion that spraying drying reclaims with the polymer powder.Because blast is the burning of quickening, therefore the oxygen concn that reduces in the spray-dryer is very important.In closed circulation, therefore the part of the gas after polymer powder reclaims can keep lower oxygen concn once more by heater heats, and the possibility of dust outburst is low.
; though open the closed cycle technology that has proposed in the clear 47-7125 communique dried 50vol% to the 80vol% gas circulation of washing composition the spy; but owing to there is not condenser; so moisture evaporated raises the water vapour ratio of the recycle system in moisture eliminator, in the recycle system, particularly water vapour can condense in the powder collection device.If improve export department's temperature of spray-dryer in order to prevent such condensing, then when the spraying drying polymer emulsion, polymer powder is known from experience attached on the wall or the problems such as export department obstruction of powder at moisture eliminator takes place, thereby is not suitable for.In addition, when the water vapour ratio of the inlet portion of spray-dryer becomes the important factor of the resulting polymer powder quality of decision, just with the water vapour ratio of the dried gas circulation amount control of washing composition spray-dryer inlet portion.But owing to do not have condenser, the water vapour ratio of feasible intrasystem oxygen concn of Control Circulation simultaneously and spray-dryer inlet portion, thereby be not suitable for.
In addition, when adopting closed round-robin spraying drying, be necessary to make the moisture of the amount of moisture phasor of crossing with the moisture eliminator drying by condenser condenses, along with increasing with moisture eliminator exsiccant treatment capacity, condensation number in the condenser increases, must adopt large-scale device for condenser and auxiliary facility (refrigeration agent producing apparatus etc.) thereof, thereby be not suitable for.
Open in the clear 60-110301 communique the spy, proposed to adopt the method for gas circulation formula spray drying unit control oxygen concn and recycle gas pressure, but must supply with N
2Thereby, increased generation N
2The cost of gas also is not suitable for.
Summary of the invention
Problem of the present invention relates to from polymer emulsion the drying process with atomizing that reclaims polymer powder, provide the temperature of the export department of spray-dryer to be in the non-cohesive wall of polymer powder and in specific range of temperatures that powder stops up does not take place for the export department of spray-dryer, carry out oxygen concn in spraying drying and the spray-dryer lower than particular concentration, and can adopt the polymer recovery processes of small-sized condenser.
Polymer recovery processes of the present invention, it is characterized in that, with heated air in spray-dryer internal spraying dry polymer emulsion reclaims the polymkeric substance in the polymer emulsion as powder method, after the part of polymer powder waste gas after the Separation and Recovery from polymer emulsion supplied with condenser and make condensate moisture, import in the direct flame heater and heat, carry out recirculation.
In aforesaid method, the preferred intrasystem oxygen concn of Control Circulation (volume %) is below 10vol%.
In addition, the temperature of preferably controlling spray-dryer export department is for than below the high 15 ℃ temperature of the minimum film-forming temperature of polymer emulsion.
In addition, preferably above-mentioned condenser will be supplied with more than the 60vol% of waste gas.
The temperature of preferred control condensator outlet by under be limited to 35 ℃, on be limited to below the temperature than low 5 ℃ of the temperature of condenser inlet.
In addition, preferably by being located at the exhausted air quantity below the drain passageway discharge 40vol% that possesses outlet valve between spray-dryer and condenser.
Description of drawings
Fig. 1 is the sketch of the recovery method of polymkeric substance of the present invention.
Embodiment
Below describe the present invention in detail with Fig. 1.
In the recovery method of Li polymkeric substance, recycle gas moves according to the order of spray-dryer 1, condenser 2, direct flame heater 3 as shown in the figure, turns back to again to carry out recirculation in the spray-dryer 1.
In addition, connect by gas circulation path 4 between spray-dryer 1 and the condenser 2, in its way, establish powder collection device 11, gas blower 12, and connect the drain passageway 14 that possesses vent valve 13.
In addition, connected by gas circulation path 5 between condenser 2 and the direct flame heater 3, connection possesses the drain passageway 19 of vent valve 18 in its way, and establishes gas blower 20.
In addition, connect by gas circulation path 6 between direct flame heater 3 and the spray-dryer 1, in its way, establish gas blower 21 and strainer 22.
In the present invention, direct flame heater 3 is will be burnt by updraft by the recycle gas that condenser 2 described later is supplied with to make the device of heated air.Preferably, to satisfy the minimal amount of incendiary by the outer fueling of the recycle system with as the air of combustion-supporting gas, by combustion fuel heating cycle gas.Combustion-supporting gas also can be supplied with in the recycle system, but the extremely low occasion of the oxygen concn in the recycle system is particularly preferably supplied with outside system.Fuel can be the geseous fuel of representative or be the liquid fuel of representative in order to kerosene in order to Sweet natural gas.
With such direct flame heater, can reduce the oxygen concn in the recycle system.
In the present invention, in spray-dryer 1, carry out the spraying and the drying of polymer emulsion with the gas of direct flame heater 3 heating.This spray-dryer 1 is established micro-granulating device 7 and inlet portion 8 at least on the top of spray-dryer 1.
Also can carry out the Separation and Recovery of polymer powder by the tripping device that other approach is established to the cycle gas mixture that contains polymer powder and transpiring moisture, but preferably set out oral area 23, in spray-dryer 1, carry out the recovery of polymer powder in the bottom of spray-dryer 1.
Above-mentioned micro-granulating device 7 is with the device in the polymer emulsion spraying importing spray-dryer 1.
Above-mentioned inlet portion 8 is to import the device that makes by the polymer emulsion exsiccant heated air of micro-granulating device 7 sprayings.It is arranged so that from direct flame heater 3 and directly contacts with polymer emulsion by the heated air that gas circulation path 6 transmits.
Preferably, the polymer emulsion of heated air and spraying flows to the bottom from the top decline of spray-dryer 1.
In the present invention, the temperature of export department 23 is important, and the spray amount of temperature, gas import volume in the inlet portion 8 and micro-granulating device 7 by control inlet portion 8 can be controlled the temperature of export department 23.For example, in the occasion of the temperature that will improve export department 23, can be separately or combination improve inlet portion 8 temperature, increase by the gas import volume of inlet portion 8, reduce operations such as emulsion spray amount by micro-granulating device 7.
The temperature of export department 23 wishes to be controlled at than below the high 15 ℃ temperature of the minimum film-forming temperature of polymer emulsion.When higher, may cause polymer powder, the obstruction of powder perhaps takes place in export department 23 attached on the wall than this temperature.
In addition, the lower limit of the temperature of export department 23 is not done special restriction, but preferably is higher than 50 ℃.This be since below 50 ℃ the time powder dry insufficient, can not meet the demands.
When the minimum film-forming temperature of polymer emulsion is meant and forms film by polymer emulsion, can form the minimum temperature of transparent continuous filminess here.The occasion of the composition homogeneous in particle, the minimum film-forming temperature almost second-order transition temperature with polymkeric substance are identical.
, the determinative of powder structure is the sticking power on the polymer particle top layer of polymer emulsion, and we are clear: the sticking power on this particle top layer is by the relation decision of " second-order transition temperature on particle top layer " and " temperature on particle top layer ".
In the polymer emulsion of multilayer polymer structure, with " second-order transition temperature on particle top layer " is that minimum film-forming temperature is as the criterion, the temperature of export department 23 by control spray-dryer 1, sticking power that just can controlling polymers particle top layer, prevent above-mentioned polymer powder in the obstruction of the adhering to of wall, export department 23, dry insufficient etc., thereby obtain good polymer powder.
As the measuring method of the minimum film-forming temperature of above-mentioned polymer emulsion, at first, establish heating or refrigerating unit at the two ends of horizontally disposed aluminum plate, make to have thermograde on the aluminum plate.Then, have on the aluminum plate of thermograde the thin polymer emulsion of expansion equably, the minimum temperature that polymer emulsion forms the transparent continuous film is measured in dry back, with it as minimum film-forming temperature.
In addition, in order to prevent the oxidation in spray-dryer 1, also can in the polymer emulsion of spraying, add suitable oxidation inhibitor or additive etc. and carry out spraying drying.
For powder characteristics such as the resistance to blocking that further improves the resulting polymers powder, loose densitys, also can add inorganic filler such as silicon, mica, salt of wormwood or polyacrylic ester, polyvinyl alcohol, polyacrylamide etc. and carry out spraying drying.
In addition, the global shape of spray-dryer 1 and capacity are not done special qualification, and the small-scale level of using from the laboratory can be used to the extensive level of industrial usefulness.
Inject the polymer emulsion of micro-granulating device 7, can enumerate: make aromatic vinyl base system monomer, acrylic monomer, ethene be unsaturated carboxylic acid be monomer, unsaturated carboxylic acid alkyl ester be monomer, ethylene halide base system monomer, maleic anhydride contract imines be one or more copolymerization, seeding polymerization or graft polymerization such as monomer, compoundization etc. resultant.In addition, also can use under the situation that has rubbery copolymers such as diene multipolymer or acrylic rubber shape multipolymer, with unsaturated nitro monomer, (first) basic acrylate monomer, aromatic vinyl base system monomer or can be with one or more polymerizations such as the monomers of their copolymerization and the graft copolymer that obtains, for example acrylonitrile-butadiene-styrene copolymer, MBS etc.
The polymerization process of polymer emulsion is not done special qualification, can adopt general known emulsion polymerization method.In addition, also can and use linking agents such as Vinylstyrene, 1,3-butylene dimethacrylate, allyl methacrylate(AMA), epihydric alcohol methylpropenoic acid ester, thio-alcohol, terebene class chain-transfer agent.
The initiators for polymerization that uses is not done special qualification, but can use with water-soluble persulfuric acid such as Potassium Persulphate, Sodium Persulfate, ammonium persulphates, the diisopropyl benzene hydrogen peroxide, to the Meng organo-peroxide such as alkane hydrogen peroxide, isopropyl benzene hydroperoxide, tertbutyl peroxide as the redox series initiators of composition.
In addition, above-mentioned emulsion both can be single, but also can be the mixture of multiple emulsion.
The mixture of the recycle gas that contains polymer powder and transpiring moisture that will discharge from venting port 10 is sent to powder collection device 11, is separated into powder and waste gas.Powder collection device 11 is made up of cyclone scrubber and cloth envelop collector.
Here, so-called waste gas is meant the mixture of the recycle gas that contains powder and transpiring moisture that will discharge from the gas discharge outlet 10 of spray-dryer 1, by the later gas of Separation and Recovery powder only such as cyclone scrubber and cloth envelop collector.
Be sent to drain passageway 14 and the condenser 2 that possesses outlet valve 13 by gas blower 12 from powder collection device 11 expellant gas.
Preferably, the gas of 1～40vol% of waste gas is discharged from the drain passageway 14 that possesses outlet valve 13.Discharge can reduce the condensation number of being handled by condenser 2.But, the waste gas of discharging from drain passageway 14 than 40vol% for a long time, the oxygen concn in the recycle system can surpass 10vol%, thereby is not suitable for.
From the waste gas output of drain passageway 14,19, form by the part of the combustion exhaust amount of discharging, combustion-supporting gas and the part of exsiccant water vapour is discharged this amount separately spray-dryer 1 part from direct flame heater 3.In addition, in order to reduce the condensation number of handling in the condenser 2, preferably between spray-dryer 1 and condenser 2, establish the drain passageway 14 that possesses outlet valve 13.
In the present invention, wish with direct flame heater 3 heating, the oxygen concn in the recycle system to be become below the 10vol% by after will supplying with condenser 2 condensed moisture above the 60vol% gas of waste gas.
If the exhausted air quantity of supplying with condenser 2 is when 60vol% is following, burning or dust explosion by the generation of the autoxidation in the spray-dryer 1 will may take place, thereby be not suitable for above 10vol% in oxygen concn in the spray-dryer 1 sometimes.Particularly, wish that oxygen concn is below 5vol% in the occasion of the polymkeric substance of dry autoxidation.
Condenser 2 is with drying in spray-dryer 1 and moisture evaporated is condensed, and makes the part of the moisture in the recycle gas be discharged to the outer device of the recycle system.Used condenser 2 also can use indirect refrigerative condenser, multitube type condenser etc. for example, but preferably especially use direct refrigerative condenser, for example wet scrubber etc.
If condenser 2 can be discharged moisture outside the recycle system, therefore can reduce the temperature of the export department 23 of spray-dryer 1, thereby reduce attached to the amount of polymers in the export department 23.
In addition, in the present invention, the temperature of control condensator outlet 16 is very important, control by under be limited to 35 ℃, below the supreme temperature that is limited to than low 5 ℃ of the temperature of condenser inlet 15.The temperature of preferred condensator outlet 16 is got more than 40 ℃.
This be because, if the temperature of condensator outlet 16 is lower than 35 ℃, the condensation number of being handled by condenser 2 increases, and causes the large-scale condenser of needs, thereby is not suitable for.
In addition, if the temperature of condensator outlet 16 be to hang down 5 ℃ temperature when above than the temperature at condenser inlet place 15, transpiring moisture in the recycle gas can not condense, the humidity of recycle gas is raise, the result worries that the water vapour from gas discharge outlet 10 expellant gas of spray-dryer 1 condenses, and therefore is not suitable in the powder collection device 11 of cyclone scrubber bag filter etc.Preferably the water vapour ratio from the recycle gas that condensator outlet 16 is discharged is 5.6vol%～57.0vol%.
Thereby the temperature of condensator outlet 16 is the temperature of refrigeration agent, wish according to the temperature that makes condensator outlet 16 by under be limited to 35 ℃, supreme being limited to than suitable decision below the temperature of low 5 ℃ of the temperature of condenser inlet 15.
As mentioned above, the temperature by control condensator outlet 16 diminishes the temperature difference between condenser inlet 15 and the condensator outlet 16, just can limit the treatment capacity of condenser 2 and uses little, the cheap small-sized condenser 2 of heat transfer area.
Under steady state, must and append the steam vapour amount of steam vapour amount same amount contained in the gas with steam vapour amount in the combustion exhaust of the steam output of spray-dryer 1 and direct flame heater 3, condense by drain passageway 14,19 with by condenser 2 and discharge outside the circulating system.
Here, it is the air of supplying with outside the recycle system that what is called is appended gas, is supplied with when spray-dryer moves by direct flame heater 3 at recycle gas.
The recycle gas that condenser 2 comes out heats once more with direct flame heater 3, mixes with the gas of being supplied with by gas blower 21 that appends, and becomes desiccant heated air.Heated air imports the inlet portion 8 of spray-dryer 1 by strainer 22 backs.Its middle filtrator 22 works the particulate effects such as carbon black dust of removing in the heated air.
Embodiment
Followingly specify the present invention according to embodiment.
(embodiment 1)
With technology shown in Figure 1, reclaim polymer powder with following device.
Spray-dryer 1 uses the internal diameter of its vertical tube part to be 3.5m, and the height of vertical tube part is that the height of 4m, conus portion is 2.8m.On micro-granulating device 7, use rotating-disk (15000 rev/mins of rotating speeds).
Condenser 2 uses by heat exchange minister 1.0m, baffle interval 0.184m, heat exchanger external diameter 0.31m, heat exchange single tube external diameter 0.026m, the several 66 multitube type condensers with baffle plate that constitute of single tube.
The composition of the polymer emulsion that uses in spray-dryer (weight %) is: methyl methacrylate 84%, butyl acrylate 16%, n-octyl mercaptan 0.0057%, wherein solid-state ratio (weight %) is 37.8%.The minimum film-forming temperature of this polymer emulsion is 66 ℃.This polymer emulsion is delivered in the spray drying unit 1 with 88.4 kilograms/hour speed, reclaimed the polymkeric substance in the emulsion.
The water ratio of the temperature of the temperature of the cyclic drying gas volume of this moment, the temperature of moisture eliminator inlet portion 8, dryer export portion 23, the output of outlet valve 13,19, condenser inlet 15, the temperature of condensator outlet 16, absolute humidity, polymer powder is as shown in table 1.
Table 1
| Embodiment 1 | Comparative example 1 | Comparative example 2 | Comparative example 3 | Embodiment 2 | ||
| Minimum film-forming temperature | [℃] | ??66 | ??66 | ??66 | ??66 | ??66 |
| The emulsion amount | [kg/hr] | ??88.4 | ??88.4 | ??88.4 | ??88.4 | ??88.4 |
| The dry gas scale of construction of moisture eliminator inlet | [kg/hr] | ??2220 | ??2220 | ??2220 | ??2220 | ??2220 |
| Dryer inlet temperature | [C°] | ??135 | ??135 | ??135 | ??135 | ??160 |
| Moisture eliminator inlet absolute humidity | [kg/kg] | ??0.069 | ??0.043 | ??0.126 | ??0.069 | ??0.069 |
| The dryer export temperature | [℃] | ??75 | ??75 | ??75 | ??75 | ??100 |
| Dryer export absolute humidity | [kg/kg] | ??0.094 | ??0.068 | ??0.151 | ??0.094 | ??0.094 |
| The rate of discharge of outlet valve | [％] | ??3.4 | ??50 | ??20 | ??-- | ??3.4 |
| The dry gas scale of construction that outlet valve is discharged | [kg/hr] | ??76 | ??1110 | ??444 | ??-- | ??76 |
| The dry gas scale of construction of condenser inlet | [kg/hr] | ??2144 | ??-- | ??-- | ??2220 | ??2144 |
| The condenser inlet temperature | [℃] | ??72 | ??-- | ??-- | ??72 | ??72 |
| The condensator outlet temperature | [℃] | ??50 | ??-- | ??-- | ??50 | ??50 |
| Condensator outlet absolute humidity | [kg/kg] | ??0.087 | ??-- | ??-- | ??0.087 | ??0.087 |
| The dry gas scale of construction of calorifier inlets | [kg/hr] | ??2144 | ??1110 | ??1776 | ??2220 | ??2144 |
| Calorifier inlets absolute humidity | [kg/kg] | ??0.087 | ??0.068 | ??0.151 | ??0.087 | ??0.087 |
| Append the dry gas scale of construction | [kg/hr] | ??78.4 | ??1039 | ??378 | ??-- | ??78.4 |
| Append absolute humidity of gas | [kg/kg] | ??0.012 | ??0.012 | ??0.012 | ??-- | ??0.012 |
| Moisture eliminator inlet oxygen concn | [％] | ??5.0 | ??18.7 | ??17.0 | ??2.0 | ??5.0 |
| The water ratio of polymer powder | [％] | ??0.5 | ??0.6 | ??1.8 | ??0.5 | ??0.4 |
The dry gas scale of construction of appending contains combustion-supporting gas.
Below describe operational conditions in detail.
With direct flame heater 3 heating cycle gases, making free air temperature is that 25 ℃, the air of relative humidity 60% mix with the recycle gas of heating, by strainer 22, imports in the spray-dryer 1.The oxygen concn of this air-supply gas is 5vol%.At spray-dryer 1 internal spraying, the powder collection device 11 that constitutes by powder relief outlet 9 with by the cyclone scrubber cloth envelop collector reclaims polymer powder with 33.4 kilograms/hour amount with polymer emulsion.The water ratio of the polymer powder of gained is 0.5wt%.Recycle gas separates with powder in the powder collection device 11 that is made of the cyclone scrubber bag filter, delivers in the gas drain passageway 14 and condenser 2 that possesses outlet valve 13 with gas blower 12.The temperature of the recycle gas of condensator outlet 16 is controlled to be 50 ℃.The heat transfer area of condenser 2 is 5.4m
2, condensation number is 53.19 kilograms/hour, even use the water coolant of recooling tower, the condensation ability of condenser 2 also is sufficient.
Consequently: the polymer powder that adheres to the export department 23 of spray-dryer 1 is few, and the oxygen level of the inlet portion 8 of spray-dryer 1 is 5vol%, and the incendiary possibility that dust explosion and autoxidation cause is low, can move safely.
(comparative example 1)
, as bypass condenser inlet 15 is connected with condensator outlet 16 usefulness conduits with condenser 2,, uses the technology identical, reclaim the polymer powder identical with embodiment with embodiment except that the rate of discharge (volume %) of outlet valve 13 is 50%.With operational conditions with the results are shown in table 1.
Consequently: the oxygen concn to the air-supply gas of spray-dryer 1 can not be reduced to below the 18.7vol%, can not eliminate the danger of dust explosion.
(comparative example 2)
Except that the rate of discharge (volume %) of outlet valve 13 becomes 20%, use the technology identical with comparative example 1, reclaim the polymer powder identical with embodiment.With operational conditions with the results are shown in table 1.
Consequently: the oxygen concn to the air-supply gas of spray-dryer 1 can not be reduced to below the 17.0vol%, can not eliminate the danger of dust explosion.In addition, the water ratio of the polymer powder of gained is 1.8 weight %, and water ratio exceeds technical specifications.
(comparative example 3)
Except using heating medium to replace direct flame heater, append and add in the gas the nitrogen as the fin tube type indirect heater of the water vapour of 2.1MPa, use and the same technology of embodiment, reclaim and the same polymer powder of embodiment.With operational conditions with the results are shown in table 1.
In this comparative example, though be reduced to 2.0vol%, to compare with embodiment to the oxygen concn of the air-supply gas of spray-dryer 1, running cost rises, and device is maximized.
(embodiment 2)
Temperature and moisture eliminator air output except change inlet portion 8, make the temperature of the export department 23 of spray-dryer 1 become 100 ℃ (more than 66 ℃ high 15 ℃ the temperature of minimum film-forming temperature than polymer emulsion 1) in addition, with the condition operation identical, reclaim 32.1 kilograms/hour polymer powder the powder recovery 11 that can constitute from powder relief outlet 9 with by the cyclone scrubber cloth envelop collector with embodiment 1.
Adopt polymer recovery processes of the present invention, owing to can the intrasystem oxygen concn of Control Circulation be low value, and the polymkeric substance that adheres to the export department 23 of spray-dryer is few, and condenser can use cheap packaged unit, thus can be spray-dryer 1 in safety, stable, make the solids of energy autoxidation at an easy rate.
Claims (6)
1. the recovery method of polymkeric substance, it is characterized in that, make in the method that the polymkeric substance in this polymer emulsion reclaims as powder in spray-dryer internal spraying dry polymer emulsion with heated air, the part of polymer powder waste gas after the Separation and Recovery from polymer emulsion is supplied with condenser make condensate moisture, import in the direct flame heater then and heat, carry out recirculation.
2. the recovery method of polymkeric substance according to claim 1 is characterized in that, the intrasystem oxygen concn of Control Circulation (volume %) is below 10vol%.
3. the recovery method of polymkeric substance according to claim 1 and 2 is characterized in that, the temperature of controlling above-mentioned spray-dryer export department is for than below the high 15 ℃ temperature of the minimum film-forming temperature of polymer emulsion.
4. according to the recovery method of each described polymkeric substance of claim 1～3, it is characterized in that, will supply with above-mentioned condenser more than the 60vol% of waste gas.
5. according to the recovery method of each described polymkeric substance of claim 1～4, it is characterized in that, the temperature of controlling above-mentioned condensator outlet by under be limited to 35 ℃, below the supreme temperature that is limited to than low 5 ℃ of the temperature of this condenser inlet.
6. according to the recovery method of each described polymkeric substance of claim 1～4, it is characterized in that, discharge amount below the 40vol% of above-mentioned waste gas by being located at the drain passageway that possesses outlet valve between spray-dryer and condenser.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021530297A CN100357006C (en) | 2002-11-29 | 2002-11-29 | Process for reclaiming polymer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021530297A CN100357006C (en) | 2002-11-29 | 2002-11-29 | Process for reclaiming polymer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1504252A true CN1504252A (en) | 2004-06-16 |
| CN100357006C CN100357006C (en) | 2007-12-26 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB021530297A Expired - Lifetime CN100357006C (en) | 2002-11-29 | 2002-11-29 | Process for reclaiming polymer |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20150000156A1 (en) * | 2013-06-27 | 2015-01-01 | Anaergia Inc. | Spray dryer exhaust treatment and anaerobic digester |
| CN105597348A (en) * | 2016-02-03 | 2016-05-25 | 山东东临新材料股份有限公司 | Efficient multifunctional polymer emulsion drying equipment |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60110301A (en) * | 1983-11-17 | 1985-06-15 | Oogawara Kakoki Kk | Controlling method for circulating gas in gas circulating type spray dryer |
| FR2603890B1 (en) * | 1986-09-12 | 1988-11-18 | Atochem | PROCESS FOR THE PREPARATION OF VINYL CHLORIDE HOMO- AND COPOLYMERS SUITABLE FOR GIVING PLASTISOLS |
| JP2001329067A (en) * | 2000-05-19 | 2001-11-27 | Mitsubishi Rayon Co Ltd | Manufacturing method of acrylic polymer |
-
2002
- 2002-11-29 CN CNB021530297A patent/CN100357006C/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20150000156A1 (en) * | 2013-06-27 | 2015-01-01 | Anaergia Inc. | Spray dryer exhaust treatment and anaerobic digester |
| CN105597348A (en) * | 2016-02-03 | 2016-05-25 | 山东东临新材料股份有限公司 | Efficient multifunctional polymer emulsion drying equipment |
| CN105597348B (en) * | 2016-02-03 | 2018-01-12 | 山东东临新材料股份有限公司 | A kind of high-efficiency multi-function polymer emulsion drying equipment |
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| Publication number | Publication date |
|---|---|
| CN100357006C (en) | 2007-12-26 |
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