GB2049899A - Process for drying vinyl chloride polymer wet cake and drier therefor - Google Patents
Process for drying vinyl chloride polymer wet cake and drier therefor Download PDFInfo
- Publication number
- GB2049899A GB2049899A GB8009840A GB8009840A GB2049899A GB 2049899 A GB2049899 A GB 2049899A GB 8009840 A GB8009840 A GB 8009840A GB 8009840 A GB8009840 A GB 8009840A GB 2049899 A GB2049899 A GB 2049899A
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- GB
- United Kingdom
- Prior art keywords
- wall
- jets
- gas
- pulsed
- chamber
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Classifications
-
- H—ELECTRICITY
- H05—ELECTRIC TECHNIQUES NOT OTHERWISE PROVIDED FOR
- H05B—ELECTRIC HEATING; ELECTRIC LIGHT SOURCES NOT OTHERWISE PROVIDED FOR; CIRCUIT ARRANGEMENTS FOR ELECTRIC LIGHT SOURCES, IN GENERAL
- H05B6/00—Heating by electric, magnetic or electromagnetic fields
- H05B6/64—Heating using microwaves
- H05B6/78—Arrangements for continuous movement of material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F33/00—Other mixers; Mixing plants; Combinations of mixers
- B01F33/40—Mixers using gas or liquid agitation, e.g. with air supply tubes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B13/00—Conditioning or physical treatment of the material to be shaped
- B29B13/06—Conditioning or physical treatment of the material to be shaped by drying
- B29B13/065—Conditioning or physical treatment of the material to be shaped by drying of powder or pellets
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F6/00—Post-polymerisation treatments
- C08F6/008—Treatment of solid polymer wetted by water or organic solvents, e.g. coagulum, filter cakes
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B3/00—Drying solid materials or objects by processes involving the application of heat
- F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
- F26B3/06—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried
- F26B3/08—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed
- F26B3/092—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed agitating the fluidised bed, e.g. by vibrating or pulsating
- F26B3/0926—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed agitating the fluidised bed, e.g. by vibrating or pulsating by pneumatic means, e.g. spouted beds
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B3/00—Drying solid materials or objects by processes involving the application of heat
- F26B3/32—Drying solid materials or objects by processes involving the application of heat by development of heat within the materials or objects to be dried, e.g. by fermentation or other microbiological action
- F26B3/34—Drying solid materials or objects by processes involving the application of heat by development of heat within the materials or objects to be dried, e.g. by fermentation or other microbiological action by using electrical effects
- F26B3/343—Drying solid materials or objects by processes involving the application of heat by development of heat within the materials or objects to be dried, e.g. by fermentation or other microbiological action by using electrical effects in combination with convection
-
- H—ELECTRICITY
- H05—ELECTRIC TECHNIQUES NOT OTHERWISE PROVIDED FOR
- H05B—ELECTRIC HEATING; ELECTRIC LIGHT SOURCES NOT OTHERWISE PROVIDED FOR; CIRCUIT ARRANGEMENTS FOR ELECTRIC LIGHT SOURCES, IN GENERAL
- H05B6/00—Heating by electric, magnetic or electromagnetic fields
- H05B6/64—Heating using microwaves
- H05B6/78—Arrangements for continuous movement of material
- H05B6/784—Arrangements for continuous movement of material wherein the material is moved using a tubular transport line, e.g. screw transport systems
Abstract
A process for drying vinyl chloride polymer wet cake 7 of water content above 23% by weight comprises (a) passing a pulsed flow 13 of drying gas (air) through a cake located in a fluid bed drier having a fluidising chamber wall of curved, preferably circular, horizontal cross-section, the pulsed flow of gas entering through the distributor plate of the drier, while injecting a plurality of pulsed jets of a non-wetting gas (air) (not shown) through the cake which jets enter the fluidising chamber at the wall thereof, wherein the jet directions in the horizontal plane are within 15 DEG , preferably within 5 to 10 DEG , of being tangential to the wall at the position of entry of the jets into the chamber, so that the cake undergoes boiling- type agitation, and (b) when the water content of the cake has fallen to <23% by weight, replacing the pulsed flow of gas through the distributor plate with a continuous flow of drying gas (air) so that the cake undergoes a fluidised agitation. In a preferred embodiment, where very rapid drying is required, the wet cake is additionally subjected to microwave irradiation 12. <IMAGE>
Description
SPECIFICATION
Process for drying vinyl chloride polymer wet cake and drier therefor
The present invention relates to a process of drying a vinyl chloride polymer wet cake in a fluid bed drier and to a fluid bed drier for effecting such drying.
It is well-known to dry vinyl chloride polymer wet cake in a fluid bed drier using a drying fluidising stream of a hot gas -- usually air.
However, we have found that with conventional fluid bed driers it is not possible to employ wet cake having water content of greater than about 23% by weight (based on polymer plus water) because serious chanelling ("rat-holing") occurs in the cake, so that the main mass of material in the fluidising chamber stagnates and is not properly dried. In view of this we have been limited, when operating a fluid bed drier, to using polymer slurry dewatering equipment which yields vinyl chloride polymer wet cake of water content 6 23%, e.g.
centrifugation equipment which generally provides vinyl chloride polymer wet cake of water content within the range 18 to 23% by weight.
However it would be desirable to have the option of using other dewatering techniques which might result in polymer wet cake of water content greater than 23% by weight. For example, centrifugation equipment is not readily automated' whereas air pressure filtration equipment (an alternative dewatering system) could be readily automated but provides wet cake of water content approximately within the range 25 to 30% by weight which therefore cannot be dried using a conventional fluid bed drier.
We have now devised a process for drying a vinyl chloride polymer wet cake of water content greater than 23% in a fluid bed drier.
According to the present invention there is provided a process for drying a vinyl chloride polymer wet cake of water content above 23% by weight (based on the weight of water plus vinyl chloride polymer) which method comprises (a) passing a pulsed flow of a drying gas (preferably air) through the wet cake of water content above 23% by weight located in the fluidising chamber of a fluid bed drier equipped with a distributor plate, the wall of the fluidising chamber having a curved, preferably circular, horizontal crosssection, and the pulsed flow of gas entering the fluidising chamber through the distributor plate of the drier, while injecting a plurality of pulsed jets of a non-wetting gas (preferably air) through the wet cake which jets enter the fluidising chamber at the wall thereof, wherein the jet directions in the horizontal plane are within 1 50, preferably 5 to 100, of being tangential to the wall at the positions of entry of the jets into the chamber, so that the wet cake undergoes a boiling-type of agitation, and (b) when the water content of the wet cake has fallen to 6 a value within the range of 1 8%-23% by weight, replacing the pulsed flow of drying gas through the distributor plate with a continuous flow of a drying gas (preferably heated air), so that the wet cake undergoes a fluidised agitation, the wall-entering jets optionally being maintained in operation.
There is also provided according to the invention a fluid bed drier suitable for drying vinyl chloride polymer wet cake of water content greater than 23% by weight, which drier is equipped with a distributor plate and comprises a fluidising chamber having a wall of curved, preferably circular, horizontal cross-section capable of sequentially receiving a pulsed and continuous flow of a drying gas (preferably air) through the distributor plate of the drier and means for injecting a plurality of pulsed jets of a non-wetting gas (preferably air) into the fluidising chamber at the wall thereof the jets having directions in the horizontal plane within 1 50, preferably 5 to 100, of being tangential to the wall curvature at the position of entry to the jets into the chamber.
The terms "horizontal" and "vertical" as used in this specification relate to the position of the fluid bed drier when in use.
The process of the invention allows the drying of a vinyl chloride polymer wet cake of water content greater than 23%, particularly 25 to 40%, particularly preferably 25 to 30%, by weight without the formation of channels ("rat-holes") in the cake. In step (a) of the process the combination of the pulsed flows of gas entering through the distributor plate and through the wall of the fluidising chamber causes the wet cake of above 23% by weight to undergo agitation akin to a "boiling" action. While this is not a true fluidisation agitation, chanelling is avoided and the whole mass of wet cake is subjected to effective drying without the existence of stagnant areas.
When the water content of the wet cake falls to Q a value within the range 1 8%-23% by weight, the pulsed flow of gas through the distributor plate is replaced by a continuous flow of drying gas (step (b)) and the wet cake undergoes true fluidisation for the remainder of the drying operation. During step (b), the wall-entering jets are optionally maintained in operation.
The pressure of the pulsed gas flow through the distributor plate in step (a) is much higher than that of the continuous flow in step (b). We do not have equipment installed capable of measuring the pressure of the pulsed gas flow through the distributor plate but it is probably a factor of 5-10 times that of the continuous flow. The pressure of the continuous flow in step (b) may be that conventionally used to achieve fluidisation when drying vinyl chloride polymer wet cake, e.g.
100--220 limit.
The duration and spacing of the pulsed flows of gas (entering through the distributor plate and wall) is not very critical but should of course be adjusted to achieve the optimum results in any set of circumstances. In the case of the pulsed flow of gas through the distributor plate, a typical range of pulse duration is 6-10 seconds (e.g. 8 seconds) with the pulse spacing (i.e. the period when the gas flow is not being applied) typically being in the range 1-5 seconds (e.g. 1 second).
In the case of the pulsed jets of gas entering through the wall of the fluidising chamber, a typical range of pulse duration is 0.25-1.5 seconds (e.g. 0.5 seconds) with the pulse spacing typically being in the range 0.10-0.5 seconds (e.g. 0.25 seconds).
The horizontal cross-section of the wall of the fluidising chamber at level of a point of entry of a wall-entering jet should be curved e.g. elliptical or circular. Preferably the horizontal cross-section of the wall of the fluidising chamber is circular at any position along its vertical length.
Preferably there are a plurality of jets entering the fluidising chamber at various levels along its vertical length (preferably at at least 3 levels along its vertical length). Furthermore at various levels along the length of the chamber (preferably at at least 3) it is preferred that there are at least 3 jets entering the chamber in the same hoizontal plane, these jet entry positions being for example equidistant from each other, with adjacent jets entering the chamber in opposing or reinforcing directions. The jet pulses may be arranged so that they are all coincident in duration and spacing; more preferably, however, the jet pulses are staggered to a greater or lesser degree.Ideally, of course, all the jets should enter the chamber so that they are within the body of the wet cake in the chamber, so that the position of the highest jet or jets will be determined by the expected amount of wet cake in the chamber.
While the jet directions in the horizontal plane should be almost tangential to the wall curvature (within 15 , preferably within 5 to 100 of being tangential), it is preferred that they enter downwardly into the chamber at an angle of at least 150, preferably 1 5 to 300., particularly preferably 1 5 to 200, to the horizontal as measured in the vertical plane as this further improves polymer agitation and inhibits polymer being blown out of the chamber.
Where very rapid drying of the vinyl chloride polymer wet cake is required, the process of the invention is advantageously operated using microwave irradiation to provide additional heat input to the agitated wet cake. Thus the fluidising chamber can be surrounded by a microwave applicator (e.g. an aluminium or stainless steel box) provided with an inlet wave guide for delivering microwave radiation from a microwave generating source.Such an embodiment has the advantage that a very large heat flux can be imparted to the moisture in the wet cake even if the actual temperature of polymer is fairly low; thus the technique can be used to dry, very rapidly, wet cake even if the vinyl chloride polymer is held at a fairly low non-degradi ng.temperature (e.g. < 800C). Consequently this embodiment is ideal for use on a small scale to rapidly provide dry samples of polymer for control purposes ahead of the main batch being dried, using a dewatering
process yielding cake of water content greater than 23% by weight such as air pressure filtration which readily lends itself to automation (the main batch can of course be dried conventionally, e.g.
using a centrifuge to dewater the slurry). Thus, for example, we have obtained dried samples (containing < 0.2% final moisture content) weighing 2 Kg in less than half an hour using this technique.
Accordingly there is provided in a further embodiment of the invention a process for drying a vinyl chloride polymer wet cake of water content greater than 23% by weight which process is as defined above but which additionally comprises subjecting the wet cake to microwave irradiation during the agitation thereof.
There is also provided in a further embodiment of the invention a fluid bed drier which is as defined above but additionally includes means to provide microwave irradiation to the contents of the fluidising chamber.
The term "fluid bed drier" in this specification includes a spouting bed drier. In such a drier the agitating air enters the fluidising chamber through a relatively small opening at the apex of a tapered (usually conical) inlet; in more conventional fluid bed driers, the agitating air enters the fluidising chamber through much larger opening (of the same order as the cross-section of the fluidising chamber). Spouting bed driers are ideal for use for small-scale drying operations e.g. as used for obtaining control samples ahead of the main batch being dried (as described above).
By "vinyl chloride polymer" in this specification is meant a vinyl chloride homopolymer or a copolymer of vinyl chloride with up to 20% by weight thereof of an ethylenically unsaturated monomer copolymerisable therewith.
The present invention is further illustrated by the following description with reference to the accompanying drawings in which:
Figure 1 is a schematic representation of a vertical view of part of a spouting bed drier according to the invention being used to dry vinyl chloride polymer wet cake in a manner according to the invention.
Figure 2 is a schematic representation of a section along the line X-X of Figure 1.
Figure 3 is a schematic representation of a vertical view of part of a spouting bed drier not according to the invention being used to dry vinyl chloride wet cake in a manner not according to the invention.
Figure 4 is a schematic representation of the spouting bed drier of Figures 1 and 2 when encased in and being subjected to the radiation from a microwave applicator.
In Figure 1, a spouting bed drier having a fluidising chamber wall 1 of circular cross-section (made e.g. of polypropylene) which tapers conically to an air entry inlet 2 and is equipped with a distributor plate 3 is being used to dry a vinyl chloride polymer wet cake of water content 25 to 30% by weight. For convenience the agitated mass of polymer cake is not shown in
Figure 1. Pulsed jets of air (e.g. of pressure 4 or 5
Bar and duration about 0.5 seconds) are directed into the chamber through wall entry ports 4 situated at three levels'down the fluidising chamber as shown, there being three equidistantly spaced and coplanar jets at each level.The jet directions in the vertical plane, indicated by the arrows in Figure 1 are downward and such that they each form an angle A of about 1 5 to 200 to the horizontal. (Where a jet is represented by a dashed line, this indicates that the jet is behind the chamber.)
As can be seen from Figure 2, the jets at each level, which enter the fluidising chamber at the wall, are equidistantly spaced and form an angle B of about 5 to 100 with the tangent (e.g. Y-Y) to the curvature of the chamber wall at the position of entry.
While the water content of the polymer cake is above 18% by weight, a pulsed flow of air is directed into the chamber through the distributor plate 3; this is replaced by a continuous flow of air when the water content of the cake is 1 8% by weight. The wall-entering pulsed jets are maintained in operation throughout.
Although not shown, the polymer cake undergoes a boiling-type of agitation without stagnant areas when the pulsed flow of air through the distributor plate is applied, and proper fluidisation when the continuous flow of air is applied.
Figure 3 shows a spouting bed drier in use which is identical with that of Figures 1 and 2 save that it is not equipped with means for injecting pulsed wall-entering jets of air into the fluidising chamber. As can be seen, the drying pulsed flow of air forms channels 5 ("rat-holes") in the polymer wet cake 6 of water content above 23% by weight, the main bulk of which remains stagnant.
Figure 4 shows the spouting bed drier of Figure 1 and 2 in use (the pulsed wall-entering air jets not being shown for convenience) but with the additional feature that the agitated polymer wet cake 7 is being subjected to microwave radiation by being surrounded by a microwave applicator (made e.g. of sheet aluminium) having a topopening lid (not shown), the microwaves being fed into the applicator at inlet 9 through a wave guide 1 0-the microwaves being produced by a microwave generating source 11. In Figure 4 the arrows 12 (solid headed) represent the microwave radiation while the arrows 13 (non-solid headed) represent the agitating air from the distributor plate.
As an example, the spouting bed drier of Figure 4. using microwave radiation of 12 cm, 2450
MHZ and a polymer cake temperature of about 800C, was able to dry samples of wet cake (dry weight 2Kg) of water content 25 to 30% by weight to a level of approximately 0.2% by weight in 20 to 30 minutes.
Claims (21)
1. A process for drying a vinyl chloride polymer wet cake of water content above 23% by weight (based on the weight of water plus vinyl chloride polymer) which method comprises (a) passing a pulsed flow of a drying gas through the wet cake of water content above 23% by weight located in the fluidising chamber of a fluid bed drier equipped with a distributor plate, the wall of the fluidising chamber having a curved horizontal cross-section, and the pulsed flow of gas entering the fluidising chamber through the distributor plate of the drier, while injecting a plurality of pulsed jets of a non-wetting gas through the wet cake which jets enter the fluidising chamber at the wall thereof, wherein the jet directions in the horizontal plane are within 1 50 of being tangential to the wall at the positions of entry of the jets into the chamber, so that the wet cake undergoes a boiling-type of agitation, and (b) when the water content of the wet cake has fallen to < a value within the range 1 8-23% by weight replacing the pulsed flow of drying gas through the distributor plate with a continuous flow of a drying gas so that the wet cake undergoes a fluidised agitation.
2. A process according to claim 5 wherein air is the drying gas employed in steps (a) and (b) and the non-wetting gas employed in step (a).
3. A process according to either claim 1 or claim 2 wherein the wall of the fluidising chamber used in the process has a circular horizontal crosssection at any position along its vertical length.
4. A process according to any one of the preceding claims wherein in step (b) the wallentering pulsed jets of gas are maintained in operation.
5. A process according to any one of the preceding claims wherein the pulsed flow of gas through the distributor plate has a pulse duration within the range 6 to 10 seconds and a pulse spacing within the range 1 to 5 seconds.
6. A process according to any one of the preceding claims wherein the pulsed jets of gas entering through the wall of the fluidising chamber have a pulse duration within the range 0.25 to 1.5 seconds and a pulse spacing within the range 0.10 to 0.5 seconds.
7. A process according to any one of the preceding claims wherein the jet directions of the wall-entering pulsed jets of gas in the horizontal plane are within 5 to 100 of being tangential to the wall at the positions of entry of the jets into the chamber.
8. A process according to any one of the preceding claims wherein the wall-entering pulsed jets of gas enter downwardly into the chamber at an angle of 1 5 to 300 to the horizontal as measured in the vertical plane.
9. A process according to any one of the preceding claims wherein wall-entering pulsed jets of gas enter the fluidising chamber at at least 3 levels along its vertical length.
10. A process according to claim 9 wherein there are at least 3 pulsed wall-entering jets entering the fluidising chamber in the same horizontal plane at at least 3 levels.
11. A process according to claim 10 wherein the jet entry positions at each level are equidistant from each other and the jet pulses are staggered.
12. A process according to any one of the preceding claims wherein the wet cake is subjected to microwave irradiation during the agitation thereof.
13. A process according to any one of the preceding claims wherein the water content of the vinyl chloride polymer wet cake to be dried is within the range of 25 to 40% by weight (based on the weight of water plus vinyl chloride polymer).
14. A fluid bed drier suitable for drying vinyl chloride polymer wet cake of water content greater than 23% by weight, which drier is equipped with a distributor plate and comprises a fluidising chamber having a wall of curved horizontal cross-section capable of sequentially receiving a pulsed and continuous flow of a drying gas through the distributor plate of the drier and means for injecting a plurality of pulsed jets of a non-wetting gas into the fluidising chamber at the wall thereof the jets having directions in the horizontal plane within 1 50 of being tangential to the wall curvature at the position of entry of the jets into the chamber.
15. A fluid bed drier according to claim 14
wherein the wall of.the fluidising chamber has a
circular horizontal cross-section of any position along it verticai length.
1 6. A fluid bed drier according to either claim 1 4 or claim 1 5 wherein the jet directions of the wall-entering pulsed jets of gas in the horizontal plane are within 5 to 100 of being tangential to the wall at the positions of entry of the jets into the chamber.
1 7. A fluid bed drier according to any one of claims 1 4 to 1 6 wherein the wall-entering pulsed jets of gas enter downwardly into the chamber at an angle of 1 5 to 300 to the horizontal as measured in the vertical plane.
18. A fluid bed drier according to any one of claims 14 to 1 7 wherein the wall-entering pulsed jets of gas enter the fluidising chamber at at least 3 levels along its vertical length.
19 A fluid bed drier according to claim 18 wherein there are at least 3 pulsed wall-entering jets entering the fluidising chamber in the same horizontal plane at at least 3 levels.
20. A fluid bed drier according to claim 19 wherein the jet entry positions at each level are equidistant from each other.
21. A fluid bed drier according to any bne of claims 14 to 21 which includes means to provide microwave irradiation of the contents of the fluidising chamber.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB8009840A GB2049899B (en) | 1979-05-01 | 1980-03-24 | Process for drying vinyl chloride polymer wet cake and drier therefor |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB7915058 | 1979-05-01 | ||
| GB8009840A GB2049899B (en) | 1979-05-01 | 1980-03-24 | Process for drying vinyl chloride polymer wet cake and drier therefor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| GB2049899A true GB2049899A (en) | 1980-12-31 |
| GB2049899B GB2049899B (en) | 1983-03-30 |
Family
ID=26271375
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB8009840A Expired GB2049899B (en) | 1979-05-01 | 1980-03-24 | Process for drying vinyl chloride polymer wet cake and drier therefor |
Country Status (1)
| Country | Link |
|---|---|
| GB (1) | GB2049899B (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2170305A (en) * | 1985-01-25 | 1986-07-30 | British American Tobacco Co | Improvements relating to the treatment of particulate materials |
| GB2183442B (en) * | 1985-12-05 | 1989-11-08 | British American Tobacco Co | Improvements relating to the expansion of vegetable materials |
| WO1989012207A1 (en) * | 1988-06-03 | 1989-12-14 | Glatt Maschinen- Und Apparatebau Ag | Process and device for drying a particulate material |
| FR2669718A1 (en) * | 1990-11-28 | 1992-05-29 | Basf Ag | CONTINUOUS PROCESS IN A TURBULENT LAYER FOR DRYING WITH TEMPERATURE-SENSITIVE WET PRODUCTS. |
| WO1995014047A1 (en) * | 1993-11-17 | 1995-05-26 | E.I. Du Pont De Nemours And Company | Purification process |
| EP0762067A1 (en) * | 1995-09-06 | 1997-03-12 | Societe Des Produits Nestle S.A. | Method and apparatus for preventing agglomeration |
| EP0864409A3 (en) * | 1997-03-10 | 1999-02-17 | Hoechst Trevira GmbH & Co. KG | Apparatus and process for crystallizing polymer granulate |
| EP1006329A1 (en) * | 1998-12-01 | 2000-06-07 | digicolor GmbH | Process for drying raw plastic materials, and process for regenerating the drying medium |
| WO2003059593A1 (en) * | 2001-12-28 | 2003-07-24 | Union Carbide Chemicals & Plastics | Gas distribution system for non-fluid bed, bulk process vessels |
| CN110328775A (en) * | 2019-07-18 | 2019-10-15 | 南京汇科高分子材料有限公司 | It is a kind of for producing the drying box of glass edge-wrapping polyurethane combined material |
-
1980
- 1980-03-24 GB GB8009840A patent/GB2049899B/en not_active Expired
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2170305A (en) * | 1985-01-25 | 1986-07-30 | British American Tobacco Co | Improvements relating to the treatment of particulate materials |
| FR2576522A1 (en) * | 1985-01-25 | 1986-08-01 | British American Tobacco Co | PROCESS AND APPARATUS FOR TREATING PARTICLE MATERIALS |
| GB2183442B (en) * | 1985-12-05 | 1989-11-08 | British American Tobacco Co | Improvements relating to the expansion of vegetable materials |
| WO1989012207A1 (en) * | 1988-06-03 | 1989-12-14 | Glatt Maschinen- Und Apparatebau Ag | Process and device for drying a particulate material |
| FR2669718A1 (en) * | 1990-11-28 | 1992-05-29 | Basf Ag | CONTINUOUS PROCESS IN A TURBULENT LAYER FOR DRYING WITH TEMPERATURE-SENSITIVE WET PRODUCTS. |
| WO1995014047A1 (en) * | 1993-11-17 | 1995-05-26 | E.I. Du Pont De Nemours And Company | Purification process |
| EP0762067A1 (en) * | 1995-09-06 | 1997-03-12 | Societe Des Produits Nestle S.A. | Method and apparatus for preventing agglomeration |
| US5911488A (en) * | 1995-09-06 | 1999-06-15 | Nestec S.A. | Method and apparatus for preventing agglomeration |
| AU711922B2 (en) * | 1995-09-06 | 1999-10-21 | Societe Des Produits Nestle S.A. | Method and apparatus for preventing agglomeration |
| EP0864409A3 (en) * | 1997-03-10 | 1999-02-17 | Hoechst Trevira GmbH & Co. KG | Apparatus and process for crystallizing polymer granulate |
| EP1006329A1 (en) * | 1998-12-01 | 2000-06-07 | digicolor GmbH | Process for drying raw plastic materials, and process for regenerating the drying medium |
| WO2003059593A1 (en) * | 2001-12-28 | 2003-07-24 | Union Carbide Chemicals & Plastics | Gas distribution system for non-fluid bed, bulk process vessels |
| CN110328775A (en) * | 2019-07-18 | 2019-10-15 | 南京汇科高分子材料有限公司 | It is a kind of for producing the drying box of glass edge-wrapping polyurethane combined material |
| CN110328775B (en) * | 2019-07-18 | 2024-04-05 | 南京汇科高分子材料有限公司 | A drying cabinet for producing glass is bordured and is used polyurethane combined material |
Also Published As
| Publication number | Publication date |
|---|---|
| GB2049899B (en) | 1983-03-30 |
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| Date | Code | Title | Description |
|---|---|---|---|
| PCNP | Patent ceased through non-payment of renewal fee |