GB1570547A - Creación de Inventos y Patentes con Inteligencia Artificial

GB1570547A – Process for coagulating polymer latices using screw-type extruder
– Google Patents

GB1570547A – Process for coagulating polymer latices using screw-type extruder
– Google Patents
Process for coagulating polymer latices using screw-type extruder

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Publication number
GB1570547A

GB1570547A
GB47353/77A
GB4735377A
GB1570547A
GB 1570547 A
GB1570547 A
GB 1570547A
GB 47353/77 A
GB47353/77 A
GB 47353/77A
GB 4735377 A
GB4735377 A
GB 4735377A
GB 1570547 A
GB1570547 A
GB 1570547A
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GB
United Kingdom
Prior art keywords
polymer
latex
coagulant
mixture
process according
Prior art date
1976-11-15
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.)

Expired

Application number
GB47353/77A
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)

IBEC IND

Original Assignee
IBEC IND
Priority date (The priority date 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 date listed.)
1976-11-15
Filing date
1977-11-14
Publication date
1980-07-02

1977-11-14
Application filed by IBEC IND
filed
Critical
IBEC IND

1980-07-02
Publication of GB1570547A
publication
Critical
patent/GB1570547A/en

Status
Expired
legal-status
Critical
Current

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Classifications

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

B29B7/00—Mixing; Kneading

B29B7/74—Mixing; Kneading using other mixers or combinations of mixers, e.g. of dissimilar mixers ; Plant

B29B7/7476—Systems, i.e. flow charts or diagrams; Plants

B29B7/7495—Systems, i.e. flow charts or diagrams; Plants for mixing rubber

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

B29B7/00—Mixing; Kneading

B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices

B29B7/34—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices

B29B7/38—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary

B29B7/40—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with single shaft

B29B7/42—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with single shaft with screw or helix

B29B7/421—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with single shaft with screw or helix with screw and additionally other mixing elements on the same shaft, e.g. paddles, discs, bearings, rotor blades of the Banbury type

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

B29B7/00—Mixing; Kneading

B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices

B29B7/34—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices

B29B7/38—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary

B29B7/40—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with single shaft

B29B7/42—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with single shaft with screw or helix

B29B7/422—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with single shaft with screw or helix with screw sections co-operating, e.g. intermeshing, with elements on the wall of the surrounding casing

B—PERFORMING OPERATIONS; TRANSPORTING

B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL

B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING

B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor

B29C48/022—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor characterised by the choice of material

B—PERFORMING OPERATIONS; TRANSPORTING

B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL

B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING

B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor

B29C48/25—Component parts, details or accessories; Auxiliary operations

B29C48/285—Feeding the extrusion material to the extruder

B29C48/29—Feeding the extrusion material to the extruder in liquid form

B—PERFORMING OPERATIONS; TRANSPORTING

B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL

B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING

B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor

B29C48/25—Component parts, details or accessories; Auxiliary operations

B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die

B29C48/395—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die using screws surrounded by a cooperating barrel, e.g. single screw extruders

B—PERFORMING OPERATIONS; TRANSPORTING

B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL

B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING

B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor

B29C48/03—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor characterised by the shape of the extruded material at extrusion

B—PERFORMING OPERATIONS; TRANSPORTING

B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL

B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING

B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor

B29C48/12—Articles with an irregular circumference when viewed in cross-section, e.g. window profiles

B—PERFORMING OPERATIONS; TRANSPORTING

B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL

B29K—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES B29B, B29C OR B29D, RELATING TO MOULDING MATERIALS OR TO MATERIALS FOR MOULDS, REINFORCEMENTS, FILLERS OR PREFORMED PARTS, e.g. INSERTS

B29K2105/00—Condition, form or state of moulded material or of the material to be shaped

B29K2105/0005—Condition, form or state of moulded material or of the material to be shaped containing compounding ingredients

Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS

Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC

Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS

Y10S528/00—Synthetic resins or natural rubbers — part of the class 520 series

Y10S528/931—Physical treatment of natural rubber or natural rubber containing material or chemical treatment of non-rubber portion thereof, e.g. extraction of rubber from milk weed

Y10S528/934—Latex

Y10S528/936—Coagulating

Description

PATENT SPECIFICATION
( 11) 1 570 547 ( 21) Application No 47353/77 ( 22) Filed 14 Nov 1977 ( 31) Convention Application No 742 077 ( 19) ( 32) filed 15 Nov 1976 in ( 33) United States of America (US) ( 44) Complete Specification published 2 July 1980 ( 51) INT CL 3 C 08 F 6/22; C 08 C t/14//B 01 F 7/08 ( 52) Index at acceptance C 3 L BC B 1 C 19 G 4 B 1 5 C 3 W 113 201 203 204 205 213 ( 54) PROCESS FOR COAGULATING POLYMER LATICES USING SCREW-TYPE EXTRUDER ( 71) We, IBEC INDUSTRIES, INC, a corporation of the State of Delaware, United States of America, having its offices at 1271 Avenue of the Americas, New York, New York 10001 United States of America do hereby declare the invention for which we pray that a Patent may be granted to us and the method by which it is to be performed to be particularly described in and by the
following statement: –
This invention relates to a process of coagulating a polymer latex and more particularly to a process for coagulating such latex using a screw-type extruder.
As used herein, the term «polymer latex» means an emulsion of a polymer in an aqueous medium The polymer may be either a conventional synthetic rubber polymer such as a styrene-butadiene rubber (SBR), a polychloroprene rubber (neoprene), an acrylonitrilebutadiene rubber (nitrile rubber), etc, a convention naturally occuring rubber latex such as a hevea rubber, a balata rubber, a gutta percha rubber, a guayule rubber, etc, a conventional plastic polymer such as an acrylonitrile-butadiene-styrene resin (ABS resin), etc; or a mixture or any other combination thereof such as an ABS-extended SBR; and as used herein, the term «polymer» means any of the foregoing materials The term «rubber latex» as used herein means a latex of a conventional rubber polymer such as an SBR, neoprene, nitrile, hevea, balata, gutta percha, guayule, etc, which is used to make rubber The «solids content» of a polymer latex refers to the weight percent of polymer and other solids in the latex.
A polymer latex is generally the product of an emulsion polymerization of a polymerizable material, although in the case of naturally occurring rubber latices, the latex is the product of a primarily natural process.
The polymer is recovered from the polymer latex by coagulating the latex This is accomplished by mnixing the polymer latex with a coagulant which breaks down the emulsion of the polymer Any of a wide variety of conventional coagulants can be used for this purpose Known coagulants include electrolytes such as acids, salts, and aqueous solutions of acids and salts Suitable aqueous acids are aqueous H 2 SO 4, HC 1, H 3 PO 4, HC 2 H 302, and the like Aqueous H 25 04 is particularly preferred for coagulating rubber latices, and particularly SBR Suitable aqueous salt solutions are solutions of Ca(Nl O 3)2, A 2 la(SO 4)a, Na Cl, and the like.
Other known coagulants are organic solvents such as ketones (e g, acetone), alcohols (e g, ethyl alcohol, methyl alcohol, etc), and mixtures thereof Mixtures of electrolytes and organic solvents (eg, an emulsion of an alcohol in an electrolyte) may also be used as coagulants.
In the coagulation of polymer latices, complete coagulation of the latex is the desired objective The amount of coagulant required to produce complete coagulation may be an important consideration in the economics of the coagulation process Polymer latices which are easy to coagulate are frequently difficult to completely coagulate This is because the rapidly coagulating polymer encapsulates or otherwise traps uncoagulated latex and prevents coagulant from contacting the encapsulated latex as is required to complete coagulation Neoprene is an example of a polymer which is particularly troublesome in this respect.
It is also desirable to produce a coagulated polymer with low moisture content since this facilitates handling and further processing of the polymer Many known coagulation processes produce coagulated polymer with relatively high moisture content, e g, 40-50 % moisture by weight The excess liquid of the coagulation process (i e, the liquid which separates from the coagulated polymer) should also be relatively low in polymer since it is typically uneconomical to attempt to recover any polymer from this liquid and this polymer is therefore usually lost In other words, 0 I1,570,547 the coagulation process should give good separation between the coagulated polymer and the excess process liquid.
With the foregoing in mind, we provide in accordance with the invention a process for coagulating a polymer latex, characterized by forming a coagulating mixture by mixing and mechanically working the polymer latex and a coagulant under a pressure of at least 15 p sig in a chamber of an elongate substantially horizontal extruder with a rotating interrupted worm flight which advances the coagulating mixture through the chamber to extruder exit, during which advance the polymer latex coagulates, maintaining the coagulating mixture under pressure at lerst until coagulation of the polymer latex is substantially complete, and, by cooperation of segments of the interrupted worm flight and a plurality of fixed breakers, which breakers project into the chamber and pass through at least some of the interruptions between the segments of the rotating interrupted worm flight, breaking up during said mixing and mechanical working of the pressurized coagulating mixture any coagulated polymer which encapsulates uncoagulated polymer latex and releasing the encapsulated polymer latex for mixture with coagulant.
Preferably, the polymer latex and coagulant are introduced into an upstream portion of the extruder chamber under pressure, preferably by injection through fixed breakers eg stationary breaker bolts, and are mixed by the rotating interrupted worm flight to form a pressurized coagulating mixture The coagulating mixture is advanced toward an extruder exit at the downstream end of the extruder chamber by the rotating interrupted worm flight The worm flight and the breakers which project into the chamber to pass through the interruptions in at least some of the segments of the interrupted worm flight, cooperate to maintain the advancing coagulating mixture under pressure at least until coagulation of the polymer latex is substantially complete Also, the worm flight segments and breakers work the coagulating mixture to either prevent the formation of any structures of coagulated polymer which may encapsulate uncoagulated latex or break down any such structures which may have formed.
All of the polymer latex is thereby contacted with coagulant The pressure in the extruder chamber promotes adequate working of the coagulating mixture by forcing coagulated masses against one another and against the worm flight segments and breakers.
At the end of the interrupted worm flight and prior to the extruder exit the coagulated polymer may be compacted and agglomerated.
For this purpose the extruder exit is preferably constricted The coagulated polymer is then extruded via the extruder exit and the excess process liquid drains freely away from the coagulated polymer Because the polymer has been completely coagulated and also preferably compacted, the extruded polymer has relatively low moisture content.
Also, the excess process liquid is relatively low in uncoagulated polymer solids.
Objects and advantages of the invention will be more apparent from the following detailed description of the invention taken in conjunction with the accompanying drawings, in which:
Figure 1 is a partly sectional plan view of illustrative screw-type extruder apparatus suitable for carrying out the process of this invention; and Figure 2 shows a die plate suitable for use on the downstream end of the extruder of Figure 1.
As shown in Figure 1, illustrative extruder apparatus for carrying out the process of this invention includes an elongated cylindrical chamber 12 (shown partially cut away in Figure 1) with an axial feed worm or screw 14 concentrically disposed therein Screw 14 includes a central shaft 16 with a helical worm flight mounted thereon The intial portion 18 of this worm flight is continuous and has a relatively high pitch This continuous portion of the worm flight is relatively short, extending for approximately 1-1/2 turns around shaft 16 The remaining (and major) portion of the worm flight is an interrupted worm flight made up of a plurality of helical interrupted worm flight segments 20 Interrupted worm flight segments 20 may be all of approximately the same pitch, or they may decrease in pitch toward the exit end 22 of the extruder This decrease in pitch may be either gradual or by stages In the particular embodiment shown in the drawing, the first interrupted worm flight segment is of relatively high pitch, the last segment is of relatively low pitch, and the intermediate segments are of intermediate pitch At least the major portion of interrupted worm flight segments 20 are preferably of lower pitch than continuous initial portion 18.
Although screw 14 includes only a single helical worm flight as shown in the drawing, it will be understood that multiple helical worm flights may be provided on all or selected portions of shaft 16 For example, similar segments of multiple interrupted worm flights may be circumferentially spaced on each longitudinal segment of shaft 16 intermediate adjacent breaker bolts 24.
A plurality of breaker bolts 24 are mounted in chamber 12 to project into the interior of the chamber intermediate at least some, preferably a majority or all, of interrupted worm flight segments 20 In the particular embodiment shown in the drawing, two diametrically opposed longitudinal rows of breaker bolts are provided along the length of chamber 12, a respective one of the breaker 1,570,547 bolts in each row projecting into the interior of the chamber intermediate each adjacent pair of interrupted worm flight segments 20.
Additional breaker bolts may be provided (generally in longitudinal rows spaced circumferentially around chamber 12) if desired.
Although breaker bolts are shown as the stationary breaker members projecting into the interior of chamber 12 in the illustrative apparatus of the drawing, it will be understood that any other type of stationary breaker members can be employed if desired For example, breakers welded to the interior of chamber 12 can be substituted for breaker bolts 24.
The leading and trailing portions of adjacent interrupted worm flight segments 20 are spaced longitudinally along shaft 16 to permit the projecting portions 28 of breaker bolts 24 to pass therebetween when shaft 16 is rotated about its longitudinal axis However, the clearances between the leading and trailing portions of the worm flight segments and the adjacent breaker bolts are preferably relatively small (i e, of the same order of magnitude as a typical diameter of structures of coagulated polymer which may form in the coagulating mixture and encapsulate uncoagulated latex, and more preferably less than such a typical diameter) to promote adequate working of the coagulating mixture between opposing surfaces of the breaker bolts and interrupted worm flight segments Worm flight segments 20 are also preferably provided with shap leading and blunt trailing edges (only trailing edges 26 are visible in Figure 1) to further promote the working of the coagulating mixture.
Chamber 12 is stationary and preferably substantially horizontal, being supported by suitable mounting means (not shown) Shaft 16 is supported for rotation about its longitudinal axis by one or more bearing boxes (not shown) disposed along the length of the portion of shaft 16 projecting from the upstream end of chamber 12 This bearing apparatus also prevents axial motion of shaft 16 Shaft 16 is rotated by any suitable drive means (not shown), for example, an electric motor The upstream end of chamber 12 is closed by upstream closure plate 30 bolted to flange 32 on the upstream end of chamber 12 by bolts 34 Shaft 16 passes through an aperture in upstream closure plate 30 This aperture permits shaft 16 to rotate freely.
Sealing collar 36 is mounted on shaft 16 inside chamber 12 adjacent upstream closure plate 30 to seal the upstream end of the apparatus by contact with closure plate 30 and thereby substantially prevent the escape of any materials from the upstream end of the extruder.
The polymer latex to be coagulated and the coagulant are introduced into chamber 12 at points along the length of the chamber which are selected to provide thorough and complete mixing and working of these materials in the chamber in accordance with the principles of this invention Apertures or nozzles specially devoted to this purpose may be provided in chamber 12 Alternatively, it has been found convenient to employ breaker bolts such as 24 a and 24 b in Figure 1 which have been axially bored through to provide a means for introducing the polymer latex and coagulant into chamber 12 The head portions of breaker bolts 24 a and 24 b may be tapped to accept male fittings at the ends of fluid supply lines 38 and 40, respectively.
Breaker bolts 24 a and 24 b are interchangeable with any unmodified breaker bolts, thereby facilitating relocation of the points at which the polymer latex and coagulant are introduced into chamber 12.
Either the polymer latex or the coagulant may be introduced upstream of the other.
The liquids are introduced into the extruder under pressure provided by pumps (not shown) in fluid supply lines 38 and 40 Shaft 16 is rotated as mentioned above so that surfaces 26 are the trailing edges of interrupted worw flight segments 20 Screw 14 therefore mixes the latex and coagulant and forwards the resulting coagulating mixture from right to left as viewed in Figure 1 toward the extruder exit orifice in die plate 22 The advancing coagulating mixture is maintained under pressure by the cooperative action of interrupted worm flight segments and breaker bolts 24 As the mixture advances and coagulates, successive breaker bolts increasingly engage the material and resist its advance, thereby producing back pressure in the upstream portion of the chamber A constricted extruder exit in die plate 22 may also contribute to the back pressure in the extruder chamber The pressure may be maintained until the material exits from the extruder, or the pressure may be relieved prior to the extruder exit, for example, by the escape of liquid from the extruder exit In any event, the coagulating mixture is maintained under pressure in the extruder at least until coagulation of the polymer latex is substantially complete As used herein «substantially complete» coagulation means the degree of coagulation at which the coagulated polymer exits from the extruder Thus in accordance with the principles of this invention, substantially all coagulation takes place under pressure This pressure is at least about 15 p s i g, and may be substantially higher.
Screw 14 ends a short distance prior to die plate 22 to provide a compaction zone 48 in chamber 12 prior to the die plate Die plate 22 is bolted to flange 42 on the downstream end of chamber 12 by bolts 44, only one of which is shown in detail in Figure 1 Die plate 22 may have one or more exit orifices 1,570,547 of any of a variety of sizes and shapes The die plate preferably provides a constricted exit from the extruder to promote compaction of the coagulated polymer near the end of worm flight 20 and in compaction zone 48.
A die plate configuration found particularly suitable for use with an extruder having an inside barrel diameter of approximately 4-1/2 inches is shown in detail in Figure 2.
The upper portion of the orifice in this die plate (above the horizontal diameter of the plate as viewed in Figure 2) is approximately a semicircle of radius 2-1/4 inches, and the lower portion of the orifice comprises two semicircles of radius 11/16 inch The die plate has a land (thickness at the orifice) of approximately 1/4 inch The single relatively large orifice of this die plate was found to give good compaction of the coagulated polymer prior to extrusion from the apparatus.
Other die plate configurations may, of course, be used.
In operation, screw 14 is rotated at a speed in the range of about 250-500 revolutions per minute Depending on the latex being coagulated, particular speeds in this range may be preferred For coagulation of an SBR latex in the 4-1/2 inch inside diameter extruder mentioned above, a speed in the range of about 250-400 revolutions per minute is preferred For coagulation of a neoprene latex in the same extruder, a speed in the range of about 450-500 revolutions per minute is preferred.
The polymer latex and coagulant are introduced into the extruder under pressure as mentioned above The latex may be a rubber latex as that term is defined above; a latex of a plastic polymer such as ABS resin; or a mixture or any other combination thereof such as ABS-extended SBR The coagulant may be any suitable coagulant Known coagulants include electrolytes such as acids, salts, and aqueous solutions of acids and salts Suitable aqueous acids are aqueous H 2504, H Cl, HPO 4, HC 2 H,0,, and the like Aqueous H 2 SO 4 is particularly preferred for coagulating rubber latices, particularly SBR Suitable aqueous salt solutions are solutions of Ca(NO,)2, A 12 ( 504),, Na Cl, and the like.
Other known coagulants are organic solvents such as ketones (e g, acetone) and alcohols (e.g, ethyl alcohol, methyl alcohol, etc), and mixtures thereof Mixtures of electrolytes and organic solvents (e g, an emulsion of an alcohol in an electrolyte) may also be used as coagulants.
The concentrations of polymer latex and of coagulant fed into the extruder are not critical, as long as there is at least sufficient coagulant to provide complete coagulation of the polymer In general, however, the process of this invention makes it possible to reduce the amount of coagulant necessary for complete coegulation of the polymer Preferably the mixture of polymer latex and coagulant in the extruder comprises about 25 to 40 % by weight of polymer solids and about 60 to 75 % by weight of coagulant.
The polymer latex and coagulant are mixed in the extruder by screw 14 to form a coagulating mixture The coagulating mixture is advanced toward the constricted extrusion orifice in die plate 22 by screw 14 As the coagulating mixture advances, interrupted worm flight segments 20 and breaker bolts 24 cooperate to vigorously work the mixture and thoroughly intermingle the constituents of the mixture to contact all of the latex with coagulant and thereby assure complete coagulation of the latex Highly turbulent conditions are induced in the mixture by the interrupted worm flight segments and breaker bolts The back pressure produced by screw 14 advancing the coagulating mixture against the resistance provided by breaker bolts 24 insures that the constituents of the coagulating mixture are worked by the interrupted worm flight segments and breaker bolts and do not merely flow in a liquid-like manner around these elements In particular, structures of coagulated polymer which might encapsulate or trap uncoagulated latex either do not form because of the turbulent mixing and working of the coagulating mixture, or if such structures forms, they are worked and broken down by the action of the interrupted worm flights and breaker bolts to release any trapped latex for contact with coagulant For this purpose, the sharp leading edges and blunt trailing edges of interrupted worm flight segments and the small clearances between worm flight segments 20 and breaker bolts 24 are particularly effective As mentioned above, the clearances between the leading and trailing portions of worm flight segments 20 and breaker bolts 24 are preferably chosen to be of the order of magnitude of or smaller than a typical diameter of a structure which might form in the coagulating mixture to encapsulate uncoagulated latex Any such latex-encapsulating structure which is forced between the leading or trailing portion of a worm flight segment and an opposing breaker bolt is thereby broken down and the encapsulated latex is released.
At the end of screw 14 prior to die plate 22 the fully coagulated polymer is compacted and agglomerated and is extruded via the constricted extrusion orifice in die plate 22.
The compaction of the coagulated polymer forces a substantial portion of the excess process liquid from the extruder via the extrusion orifice separately from the compacted coagulated polymer This liquid drains freely from the extruded polymer The extruded polymer is therefore characterized by relatively low moisture content, typically less than about 25 % by weight Moisture contents in the range of 15-25 % by weight are most 1,570,547 frequent Also, the polymer solids content of the separately expressed excess process liquid is relatively low, typically about 5 to 1.5 % by weight.
The coagulated polymer exiting from the extruder is ready for further processing in the conventional manner; it being understood that because of the relatively low moisture content of the polymer, certain dewatering steps may be eliminated In addition, because of the more efficient use of the coagulant and the low moisture content of the extruded polymer, the p H of the extruded polymer can be more carefully controlled Advantageously, the p H of the extruded polymer is such that extensive washing of the polymer is unnecessary Typically the p H of the extruded polymer is in the range from about 6 to 8.
The following examples are provided as illustrations of the process of this invention and with no intention of limiting the invention thereto.
Example I
In this example an extruder similar to that shown in Figure 1 and having an inside diameter of 4-1/2 inches and an inside length of approximately 4 feet was used The outside diameter of worm shaft 16 was approximately 2-1/2 inches Die plate 22 was as shown in Figure 2 and described above.
Worm 14 was driven by a motor having approximately 75 horsepower.
The latex coagulated was an SBR latex known as » 1018 » and available from Polysar Limited, Sarnia, Ontario, Canada N 7 T 7 M 2.
This latex has a nominal solids content of 30.2 % by weight and a p H of 8 38 The coagulent used was 0 8 normal aqueous H 2 SO 4 Both the latex and coagulant were supplied to the extruder at ambient temperature The coagulent was introduced into the extruder near the upstream end of the extruder The latex was introduced through the fifth breaker bolt (approximately 15 inches) from the downstream end of the extruder The latex was supplied at a rate of approximately 12 5 pounds per minute and the coagulant was fed at a rate of about 3 5 pounds per minute (Substantially higher latex feed rates are believed possible with this coagulant feed rate, but the latex feed rate was limited in the test apparatus by the capacity of the latex feed pump) Worm 14 was rotated at slightly more than 300 revolutions per minute.
Coagulated rubber having a moisture content of about 15 5 % was extruded at the rate of about 402 pounds per hour The back pressure immediately prior to die plate 22 was approximately 20 p s i g The temperature of the extrudate was 90-100 ‘F The excess process liquid was approximately 99 % moisture and had a p H of approximately 1 6.
Example II
In this example the extruder used was similar to that used in Example I The latex coagulated was neoprene latex type M 1 available from Petro-Tex Chemical Corporation, 8600 Park Place Blvd, Houston, Texas 77017, having a nominal solids content of 37.7 % and a p H of 12 30 The coagulant was an aqueous solution of 1 7 % Ca(NO 3)2 and 0.4 % A 1,( 504)3 The coagulant was introduced into the extruder through the second breaker bolt from the upstream end of the extruder, and the latex was introduced through the third breaker bolt from the upstream end Both coagulant and latex were supplied at ambient temperature and at flow rates of 4 28 and 6 0 pounds per min te, respectively.
Worm 14 was rotated at approximately 475 revolutions per minute The back pressure.
just prior to die plate 22 was approximately p s i g The temperature of the extrudate was approximately 1230 F Complete coagulation took place to form rubber crumb which was discharged from the extruder with a moisture content of about 17 % The excess process liquid was approximately 1 4 % solids and had a p H of about 7 3.
Example III
In this example the extruder used was similar to that used in the preceding examples.
The latex coagulated was an SBR latex known 95 as » 1502 » available from Goodyear Tire & Rubber Company, 1144 East Market Street, Akron, Ohio 44316 This latex has a nominal solids content of 30 % by weight and a p H of 8 2 The coagulant was 0 6 N HSO The 100 coagulant was introduced into the extruder through the second breaker bolt from the upstream end of the extruder in each of the two rows of breaker bolts, and the latex was introduced through the third breaker bolt 105 from the upstream end in each of the two rows of breaker bolts Both the latex and coagulant were introduced at ambient temperature The coagulant flow rate was 12 5 to 21 pounds per minute and the latex flow rate 110 was 95 pounds per minute.
Worm 14 was rotated at approximately 275 revolutions per minute The back pressure prior to die plate 22 was 30 to 35 p s i g.
Coagulated rubber was extruded at approxi 115 mately 28 pounds per minute with a moisture content of approximately 30 % and a temperature of approximately 95 F The excess process liquid was approximately 1 5 % solids and had a p H of about 1 4 120

Claims (12)

WHAT WE CLAIM IS:-

1 A process for coagulating a polymer latex comprising forming a coagulating mixture by mixing and mechanically working the polymer latex and a coagulant under a pres 125 1,570,547 sure of at least 15 psig in a chamber of an elongate substantially horizontal extruder with rotating interrupted worm flight which advances the coagulating mixture through the chamber to an extruder exit, during which advance the polymer latex coagulates, maintaining the coagulating mixture under pressure at least until coagulation of the polymer latex is substantially complete, and, by co-operation of segments of the interrupted worm flight and a plurality of fixed breakers, which breakers project into the chamber and pass through at least some of the interruptions between the segments of the rotating interrupted worm flight, breaking up during said mixing and mechanical working ef the pressurized coagulating mixture any coagulated polymer which encapsulates uncoagulated polymer latex and releasing the encapsulated polymer latex for mixture with coagulant.

2 A process according to claim 1, wherein the polymer latex is a rubber latex.

3 A process according to claim 2, wherein the rubber latex is a styrene-butadiene rubber, a polychloroprene rubber or an acrylonitrilebutadiene rubber, or a mixture thereof.

4 A process according to any one of the preceding claims, wherein the coagulant is an electrolyte or an organic solvent, or a mixture thereof.

A process according to any one of the preceding claims, wherein the coagulant is an aqueous salt solution or an aqueous acid, or a mixture thereof.

6 A process according to claim 5, wherein the coagulant is aqueous HSO 4.

7 A process according to any one of the preceding claims, wherein the coagulant is a ketone or an alcohol or mixture thereof.

8 A process according to any one of the preceding claims, wherein the interrupted worm flight is rotated at a speed in a range of from 250 to 500 revolutions inclusive per minute.

9 A process according to any one of the preceding claims, wherein the coagulated polymer is extruded with a moisture content less than about 25 % by weight.

A process according to claim 1, wherein the polymer latex is a styrene-butadiene rubber having a solids content in a range of from about 20 to 35 % by weight, in that the coagulant is aqueous HSO and in that the coagulated polymer is extruded with a moisture content less than about 25 % by weight.

11 A process according to any one of the preceding claims, wherein the coagulated polymer is compacted immediately prior to said constricted exit from which the compacted coagulated polymer is extruded.

12 A process for coagulating a polymer latex substantially as hereinbefore described with reference to an as illustrated in the accompanying drawing.
MEWBURN ELLIS & CO, Chartered Patent Agents, & 72 Chancery Lane, London WC 2 A 1 AD, Agents for the Applicants.
Printed for Her Majesty’s Stationery Office by the Courier Press, Leamington Spa, 1980.
Published by the Patent Office, 25 Southampton Buildings, London, WC 2 A l AY, from which copies may be obtained.

GB47353/77A
1976-11-15
1977-11-14
Process for coagulating polymer latices using screw-type extruder

Expired

GB1570547A
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US4103074A
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1976-11-15
1976-11-15
Process for coagulating polymer latices using screw-type extruder

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Process for coagulating polymer latices using screw-type extruder

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1976

1976-11-15
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US05/742,077
patent/US4103074A/en
not_active
Expired – Lifetime

1977

1977-11-11
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Withdrawn

1977-11-14
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CA290,792A
patent/CA1091391A/en
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Expired

1977-11-14
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IN1603/CAL/77A
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GB47353/77A
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Expired

1977-11-14
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FR7734190A
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1977-11-14
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IT69552/77A
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1977-11-14
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1977-11-14
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1977-11-14
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BE860817A
(en)

1978-05-16

IT1091044B
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1985-06-26

FR2370573A1
(en)

1978-06-09

NL7712522A
(en)

1978-05-17

BR7707586A
(en)

1978-07-18

AU511821B2
(en)

1980-09-04

IN146138B
(en)

1979-03-03

MX4435E
(en)

1982-05-04

JPS6125721B2
(en)

1986-06-17

ZA776778B
(en)

1978-09-27

US4103074A
(en)

1978-07-25

AU3060877A
(en)

1979-05-24

JPS5361640A
(en)

1978-06-02

DE2750682A1
(en)

1978-05-24

CA1091391A
(en)

1980-12-09

ES464105A1
(en)

1978-09-01

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