CA1206694A - Method for recovering synthetic resinous latex solids - Google Patents

Abstract

Abstract of the Disclosure Latex is shear coagulated to form a paste, the paste heated and sheared to form a desired crumb; the crumb is mechanically dewatered and ground to a desired particle size. Relatively low energy consumption is a feature of the process.

Description

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METHOD FOR RECOVE:RING
SY~THETIC RESINOUS LATEX SOLIDS

Synthetic resinous materials are prepared in a variety of ways including mass polymerization, suspension polymeri~ation, solution polymerization and emulsion polymerization~ For many rssinous materials it is de-sirable that they be prepared by emulsion pol~ner-ization since the desired particle size, molecular weight or graf-ting reaction is more readily obtained by : emulsion polymerization than by other polymerization methods.

Latex solids have been recovered most frequently by adding an electrolyte to the latex, usually with heating and agitation to cause the latex particles to : agglomerate into macro particles which are readily filtered, washed and dried. Typical processes are discussed in U.S. 3,248,455; 3,345,430; and 3,438,923.
For 50m~ purposes the use of electrolyte in coagulation results in undesired retention of the emulsifier ernployed in the emulsion polymerization and often retention of at least some of the coagulation electrolyte.

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-2 To overcome the problem of electrolyte retention, nitrile polymer latexes have been coagulated by shear coagulation. In this process a latex is subjected to mechanical shear un'cil at least a major portion of the latex particles have agglomerated. With a latex solids content of about 20 to 30 weight percent, the shear coagulated product is a more or less grainy paste. U.S. 3,821,345 discloses a shear coagulation process wherein the resultant paste of a nitrile polymer latex is extruded, placed in hot water for a period of time and then washed and dried.

It would be desirable if there were available an impxoved process for the recovery of latex solids which required minimal energy and ~uantities of water and steam.

These advantages are achieved by ~he present invention in a process for the recovery of synthetic resinous thermoplastic latex solids ~rom a latex char-acterized by (A) providing a latex of a synthetic resinous thermoplastic polymer containing about 10 to 50 weight percent solids, (B) subjecting the latex to mechanical shear sufficient to transform the latex into a paste-like mass, (C) admixing the paste-like mass with steam under pressure with mechanical shear provided by the admixture of steam with said mass to thereby heat the paste-like mass above the softening point of the polymer and form a plurality of macro particles of which at least 90 weight percent are retained on an 80 mesh U.S. Sie-ve Size screen, and subsequently (D) subjecting said macro particles to mechanical working to expel at least a majority of water associated therewith.

27,779-F -2-~Z0~ 4 The process of khe present invention is operable with any synthetic resinous thermoplastic latex having solids content by weight of from about 10 to about 50 weight percent. Typically, latexes which are useful in the present process include latexes of polystyrene, polymethyl methacrylate, polybutadiene, polyisoprene, polyvinylacetate, polyvinylchloride as well as various copolymer latexes including styrene--butadiene latexes, vinylchloride-vinylacetate copolymers, vinylidene chloride-vinylchloride latexes, polymethyl-methacrylate latexes-polymethylacrylate latexes.
Latexes which particularly benefit from with the present invention are styrene-acrylonitrile-rubber latexes wherein styrene-acrylonitrile copolymer is grafted to a diene rubber substrate such as polybutadiene.

The only component in addition to the latex that is required is process stPam. Steam of commercial purity under pressures of about 25 to 400 pounds per square inch guage (170-2760 kPa) are generally satisfactory.
During the heating of the paste-like mass prepared by shear coagulation, the temperature of the solids should be raised at least to the softening point of the polymer to permit desired agglomera~ion. Therefore, the steam pressure for a particular latex must be sufficiently high to raise the polymer to its softening point.

If it is desired to dilute the latex prior to shear coagulation to provide a paste of a ~ore flowable consistency, water is employedO Usually it is desirable that such water be deionized to minimize possible introduction of ma~erials which might affect the thermal stability of the desired end product.

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.~ -4-Furth~r features and ad~antages of the present invention will become more apparent from the Drawing wherein:

Figure 1 is a simplified schematic represen-tation of the process in accordance with the present invention.

Figure 2 i5 a representation of a s~eam paste mixing device such as is employed ln Figure 1.

Figure 3 is a schematic sectional represen-tation of the steam paste mixing inlet portion of thedevice of Figure 2.

In Figure 1 there is schematically depicted an apparatus 10 suitable for the practice of the process of the present invention. The apparatus 10 comprises in cooperative combination a shear coagulator 11. The shear coagulator 11 has in association therewith a latex carrying conduit 12 which discharges a synthetic resinou~ thermoplastic latex into coagulator 11. The conduit 12 has associated therewith a steam supply conduit 13 attached to supply skeam to latex in the conduit 12 and raise the temperature to a desirable coagulating temperature; for example, 40 - 90C. The shear coagulator 11 discharges a stream of paste-like mass 14 to a mixing and forwarding apparatus 16. The mixing and forwarding apparatus 16 beneficially can be a rotary type mixer with blade~ affixed to a shaft, the blades being inclined at an angle to the shaft to provide a ~orwarding action. The mixer 16 has an inlet 17 and a discharge 18. The discharge 18 of the mixer 30 16 is in communication with a pump 19. The pump 19 27,779-F -4-`

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beneficially is a screw type pump such as is commercially available under the trade name o~ Moyno. The pump 19 has an inlet in operative communication with the discharge 18, mixing and forwarding device 16, and a discharge conduit 21 in operative communication with a steam mixing and shearing device 22. The mixing and shearing device 22 has a steam inlet 23 and an outlet 24. The mixing and shearing device 22 ~orms the paste-like mass from the pump 19 into a wet granular mass. The wet granular mass passes through the discharge 24 into a mechanical dewatering apparatus 26 having an inlet communicating with the discharge 24. The mechanical dewatering apparatus 26 has a first or solids discharge 27 and a liquid discharge line 28. The liquid discharge line 28 is in communication with a filter or screen assembly 29. The filter assembly 29 has a liquid discharge 31 and a solids discharge 32. The solids discharge 32 discharges to the inlet 17 of the mixing and forwarding ~evice 16. The solids discharge 27 passes to a grinder 33 which com~utes the solid material from the mechanical dewatering devicP 26. The particulated solids from the grinder 33 are passed through conduit 35 to a cooler such as a rotary cooler 36 having a cooling water inlet 37 and a cooling water discharge 38~ Particulate material from the cooler 36 is discharged via line 39 into a storage hopper 40 and subsequently passed from the hopper 40 through line 41 for packaged shipment and final use.

In Figure 2 there is a schematic representation of a steam-paste mixing apparatus generally designated by the reference numeral 50. The apparatus 50 is generally equivalent to the mixer designated by the reerence numeral 22 in Figure 1. The mixer 50 comprises 27,779-F -5-1~3' ~aZ(~6~i94 an inlet mixing assembly generally designated by the reference numeral 51 which comprises steam valve 52 having a steam inlet 53 and a discharge region 54. The discharge region 54 of the valve 52 is in communication with a paste inlet mixing and shearing assembly 55 having a paste inlet 56 and a high shear region 57.
The high shear region 57 has a discharge end 58 which is in full communication with a pipe section 59. The pipe section 59 remote from the high shear region 57 is connected to a reducer 61. The discharge of the reducer 61 is in communication with a backpressure valve 62.
Beneficially the valve 62 is a fluid operated pinch valve. By fluid operated pinch valve is meant a valve that comprises a housiny, a flexible tube is disposed within the housing and serves to convey fluids there-through. Space between the tube and the housing is in communication with a source of a pressurized fluid whcih can be selectively applied thereto to collapse the flexible tube and thereby close the valve or to remove at least a portion of the pressurized fluid to thereby open the valve. The valve 62 remote from the reducer 61 is in communication with conduit 63. The conduit 63 remote from the valve 62 terminates in a disentrainment chamber 64. The chamber 64 has an overhead vent 65 through which steam may escape and a bottom discharge 66 through which the solid wet par-ticulate product is withdrawn.

Figure 3 is a schematic sectional represen-tation of the steam pas~e mixing section 51 of Figure 2. Disposed within the high shear region 57 is a tube 68. The tube 68 has a first inlet end 69 and a second or discharge end 71. The tube 68 is adjustably mounted within the mixing section in such a manner that the 27,779-F -6-., ~20~;69~1L
-~ -7-location of the inlet end 69 can be axially positioned toward or away from the valve 52 and thereby vary the shearing and agitating effect o~ the steam on the latex paste-like mass provided from inlet 56.

In the practice of the process of the present invention with particular reference to the Drawing, latex is passed through conduit 12 wh~ere it is heated by steam introduced from conduit 13. The shear coagu-lator 11 is adjus~ed until a desired paste-like con-figuration is obtained. For example, a suitable shear coagulator is a butter churn of the generally horizontal cylindrical drum variety having internal blades wh:ich rotate about the axis of the drum, the blades having a clearance from the drum of about one-eighth of an :inch (3.2 mm). When temperakure of the incoming latex and rotational speed of the shear coagulator 11 have been adjusted to provide desired paste-like effluent, the paste-like mixture is passed into inlet 17 of the mixer 16. The mixer 16 provides the dual function of forwarding the paste toward the pump 14 as well as mix into the paste any solids which are returned through line 32.
In the event that the paste consistency is thicker than desired, the mixer 16 can be employed to optionally dilute the paste with water to provide a more flowable stream. The pump 19 beneficially forwards the paste through the line 21 into the s~eam mixing and shearing device 22. Such a mixing and shearing device is schematically depicted in Figures 2 and 3. When paste starts to flow, for example, through inlet 56, steam is introduced through the opening 53 and controlled by the valve 52. Pressure within the pipe section S9 is controlled in part by the appropriate opening and closing of the valve 62 and adjustment of the tube 69 27,779-F -7-~20~;6~4 until the desired crumb is obtain~d. Such a crumb con~ains a plurality of macro particles of which at least 90 weight percent are retained on an 80 mesh U.S.
Sieve size screen having 0.177 mm sieve openings, 0.119 mm diameter wire, and 34 mesh/cm. The resultant slurry preferably at a temperature below the softening temperature of the latex polymer passes from the mixer 50 through opening 66 into mechanical dewatering device such as device 26. A suitable dewatering device is a so-called expeller or expressing apparatus which basically is a screw extruder having longitudinal slots formed in the barrel thereof of width sufficient to permit water or like liquids to flow therethrough and yet sufficiently narrow to prevent solids from passing through. Roller mills and like expressing apparatus are also suitable and may be u~ed alone or in combination. The solids material discharged from the expeller is ground to a desirable size, collected if necessary by a collector such as hopper 40 and stored for future use.

For many applications it is not necessary to remove all of the water. Typically the water content of the ma~erial emerging from the mechanical dewatering device such as device 26 is about 10 to 20 weight percent. Also, it is generally desirable to prepare as large a batch charge of latex as possible since individual adjustment o~ the apparatus is usually necessary for each batch.

To illustrate further the present invention, co~eniently, mixer such as is depicted in Figure 2 for a throughput sli~htly in excess of 2,000 pounds (908 kg) o~ latex per hour employs as pipe 59 three-inch (7.6 cm)diameter stainless steel Schedule 40 pipe. A

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, .9 tube, such as tube 69, is about one inch (2.54 cm~ in diameter. The conduit 61 is a stainless steel reducer from three-inch (7.6 cm) to two-inch (5.1 cm) pipe.
The valve 62 is a nominal t~o-inch (5.1 cm) pipe size and the disentrainment chamber 64 is about eighteen inches (45.7 cm) in diameter, and operated at about atmospheric pressure.

Example 1 A plurality of latex batches were prepared containing 41 weight percent styrene, 20 weight percent acrylonitril~ and 39 percent butadiene based on latex solids. The latex particle size was about 1600 angstroms (0.16 microns) in diameter and the latexes were about 31 weight percent solids.

The range of operating conditions for the shear coagulator and average values for about fifty batches o~ latex are set forth in Table I.

TABLE I

OPERATING CON~ITIONS
MEAN
PARAMETER UNITS VALUE RANGE
Latex Feed ~ate lb/hr 2350 1200-4400 [kg/hr)(1067)(545-1998) Coagulation Temp. C 65 ~3-60 25 Hydroset Backpressure psig 60 55-75 (kPa) (415) (380-520) Hydroset Temp. C 119 86-148 ~xpeller Output lb/hr 727 250-850 Pressed Cake (kg/hr)(330) (113-386) 30 Outlet Moisture wt % 19 10-20 27,779-F -9-Example 2 Another series of latexes were prepared containing 46 weight percent butadiene, 17 percent acrylonitrile and 37 percent styrene by preparing a butadiene latex and gxafting thereon styrene-acrylonitrile to provide latexes having about 37 weight percent solids and a particle size of about 1400 angstroms (0.14 microns). The latex was coagulated at 37 percent solids and diluted in the mixing and forwarding apparatus to about 26 to 32 percent solids in order to provide a more flowable paste. The range of operating conditions and ~he mean values are set forth in Table II.

TABLE II

OPERATING CONDITIONS
MEAN
PARAMETER UNITS VALUE RANGE
___ _ Latex Feed Rate* Ib/hr 2210 900-3700 (kg/hr~(1003)(409-1680) Coagulation Temp. C 46 38-66 20 Hydroset Backpressure psig 35 10-80 (kPa) (240) (70-550) Hydroset Temp. C 95 70-115 Expeller Output lb/hr 500 280-580 Pressed Cake (kg/hr)(227) (127-263) 25 Outlet Moisture wt % 11.8% 9-14 *Coagulated paste diluted to approximately 26 to 32%
solids by weight prior to mixing and hdyrosetting.

In a manner similar to the foregoing, other synthetic resinous thermoplastic latexes are readily coagulated and dewatered.

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Claims (6)

1. A process for the recovery of synthetic resinous thermoplastic latex solids from a latex characterized by (A) providing a latex of a synthetic resinous thermoplastic polymer containing about 10 to 50 weight percent solids, (B) subjecting the latex to mechanical shear sufficient to transform the latex into a paste-like mass, (C) admixing the paste-like mass with steam under a pressure of 170 to 2760 kPa with mechanical shear provided by the admixture of steam with said mass to thereby heat the paste-like mass above the softening point of the polymer and form a plurality of macro particles of which at least 90 weight percent are retained on an 80 mesh U.S. Sieve size screen, and subsequently (D) subjecting said macro particles to mechanical working to expel at least a majority of water associated therewith.

2. The process of Claim 1 wherein the latex has polymerized therein styrene, acrylonitrile and rubber.

3. The process of Claim 1 wherein the latex is subjected to mechanical shear sufficient to form the latex into a paste-like mass at a temperature of 40° to 90°C.

4. The process of Claim 3 wherein the latex is subjected to mechanical shear in a butter churn.

5. The process of Claims 1-3 wherein the plurality of macro particles are passed through a fluid operated pinch valve prior to mechanical working.

6. A process for the recovery of synthetic resinous thermoplastic latex solids from a latex prepared by polymerization of styrene and acrylonitrile in the presence of rubber characterized by (A) providing a latex containing 10 to 50 weight percent solids, (B) subjecting the latex to mechanical shear at a temp-erature of 40° to 90°C, the mechanical shear being provided by a butter churn, and being sufficient to transform the latex into a paste-like mass, (C) admixing the paste-like mass with steam under a pressure of about 170 to 2760 kPa with additional mechanical shear provided by the admixture of steam with said mass to thereby heat the paste-like mass above the softening point of the styrene acrylonitrile rubber polymer and form a plurality of macro particles of which at least 90 weight percent are retained on an 80 mesh U.S. Sieve size screen, (D) passing the macro particles through a fluid operated pinch valve, and subsequently (E) subjecting said macro particles to mechanical working to expel at least a majority of water associated therewith.