Expandable polystyrene pellets

Claim 2

A process for manufacturing expandable polystyrene pellets comprising: (a) admixing at a temperature of from about 100° C. to about 140° C. virgin polystyrene beads having a molecular weight of less than about 200,000 and having a melt index from about 4.5 to about 5.0 with an effective minor amount of a nucleating agent for generating carbon dioxide under extrusion conditions to provide an extrusion mixture, said virgin polystyrene beads containing from about 5.9 to about 7.5 weight percent of a vaporizable expanding agent compatible with the polystyrene; (b) cooling said extrusion mixture to a temperature of from about 80° C. to about 100° C. so as to increase the viscosity of the extrusion mixture; (c) introducing the extrusion mixture into an extruder and extruding at heat plasticized mass at a temperature of from about 115° C. to about 125° C. and at a pressure of from about 1800 psi to about 2200 psi to form an unexpanded extrudate in a filamentary form; (d) drawing the extrudate away from said extruder at said temperature of from about 115° C. to about 125° C. and at said pressure of from about 1800 psi to about 2200 psi into the air at a rate of from about 1.5 to about 2 times greater than the rate of extrusion to provide a drawn extrudate having a substantially continuous, gas impervious skin integral with and covering an interior portion of the extrudate; (e) immediately cooling at least the surface of the drawn extrudate to a temperature below the vaporization temperature of the vaporizable expanding agent; (f) cutting said drawn extrudate into pellets; (g) cooling the pellets to about ambient room temperature; and (h) aging, under atmospheric pressure and ambient room temperature, the pellets by exposing the pellets to ambient atmospheric conditions for a period of time effective to provide substantially uniform dispersement of the vaporizable expanding agent throughout the interior portion of the pellets.

Claim 3

The process for manufacturing expandable polystyrene pellets of claim 1 wherein the effective minor amount of the nucleating agent admixed with the polystyrene beads is an amount of from about 0.4 to about 0.25 grams of nucleating agent per kilogram of polystyrene beads.

Claim 4

The process for manufacturing expandable polystyrene pellets of claim 2 wherein the nucleating agent is comminuted prior to mixing with the polystyrene beads.

Claim 5

The process for manufacturing expandable polystyrene pellets of claim 3 wherein the nucleating agent is selecting from the group consisting of amorphous calcium polysilicate and a mixture of citric acid and sodium carbonate.

Claim 6

The process of manufacturing expandable polystyrene pellets of claim 1 wherein the vaporizable expanding agent is an aliphatic hydrocarbon.

Claim 7

The process of manufacturing expandable polystyrene pellets of claim 5 wherein the vaporizable expanding agent is an aliphatic hydrocarbon selected from the group consisting of n-pentane, iso-pentane and mixtures thereof.

Claim 8

The process of manufacturing expandable polystyrene pellets of claim 1 wherein the cooling of the drawn extrudate comprises contacting the drawn extrudate with a cooling liquid maintained at a temperature of from about 15° C. to about 30° C. for a period of time of from about 1 to 30 seconds.

Claim 9

The process for manufacturing expandable polystyrene pellets of claim 7 wherein the cooling liquid is water, and the drawn extrudate is passed through a vessel containing said water.

Claim 10

The process for manufacturing expandable polystyrene pellets of claim 8 further comprising drying the cooled drawn extrudate to remove residual water therefrom prior to cutting the drawn extrudate into pellets.

Claim 11

The process of manufacturing expandable polystyrene pellets of claim 1 further comprising passing the pellets through a cyclone apparatus operated at ambient temperature so as to cool the pellets to a temperature of less than about 30° C., and separating the cooled pellets from fines produced during the cutting of the extrudate into the pellets prior to aging the pellets by exposure to ambient atmospheric conditions.

Claim 12

The process for manufacturing expandable polystyrene pellets of claim 10 wherein the period of time effective to achieve substantial uniform dispersement of the vaporizable expanding agent throughout the interior portion of the pellets is greater than about 1.5 hours.

Claim 13

The process for manufacturing expandable polystyrene pellets of claim 1 wherein extrusion mixture is extruded through a screw-type extruder characterized as having a melt zone, a cooling zone, and a die head, in the melt zone the extrusion mixture being heated to a temperature of from about 115° C. to about 130° C. so as to form the heat plasticized mass, in the cooling zone the heat plasticized mass being cooled to a temperature of from about 80° C. to about 100° C. to reduce the viscosity of the heat plasticized mass prior to extruding same through the die head of the extruder.

Claim 14

The process for manufacturing expandable polystyrene pellets of claim 12 wherein the virgin polystyrene beads employed to form the extrusion mixture have a molecular weight of from about 90,000 to about 150,000.

Claim 15

The process of manufacturing expandable polystyrene pellets of claim 1 wherein the aging of the pellets by exposure to ambient atmospheric condition is for a period of time of at least about 2 hours, and said pellets are characterized as having a bulk density of about 36 pounds per cubic foot, and said pellets, upon heating under condition of maximum volume increase of the pellets, provide expanded particles having a bulk density of about 0.8 pounds per cubic foot, said particles having a substantially gas impervious skin integral with and covering an interior portion of the particle, said interior portion containing substantially uniform cells of having a cell diameter of less than about 40 microns.

Claim 16

A process for manufacturing expandable polystyrene pellets comprising: (a) admixing virgin polystyrene beads impregnated with from about 5.9 to about 7.5 weight percent of a vaporizable expanding agent and having a melt index from about 4.5 to 5.0 with from about 0.4 to about 0.25 grams of a nucleating agent per kilogram of polystyrene beads to form an extrusion mixture, said polystyrene beads having a molecule weight within the range of from about 90,000 to about 150,000; (b) introducing the extrusion mixture into an extruder, said extruder characterized as having a melt zone, a cooling zone, a die head and an extruder screw for advancing the extrusion mixture under extrusion pressure towards the die head; (c) heating the extrusion mixture in the melt zone of the extruder to a temperature of from about 115° C. to about 130° C. so as to produce a heat plasticized mass; (d) cooling the heat plasticized mass in the cooling zone of the extruder to a temperature of from about 80° C. to about 100° C. so as to increase the viscosity of the plasticized mass; (e) extruding the cooled plasticized mass into an atmospheric environment through the die head of the extruder at a temperature of from about 115° C. to about 125° C. and at a pressure of from about 1800 psi to about 2200 psi to form an unexpanded extrudate in filamentary form; (f) drawing the extrudate away from said extruder at said temperature of from about 115° C. to about 125° C. and at said pressure of from about 1800 psi to about 2200 psi into the air at a rate of from about 1.5 to about 2.0 times greater than the rate of extrusion to provide a drawn extrudate having a substantially continuous gas impervious skin integral with and covering an interior portion of the drawn extrudate; (g) immediately passing the drawn extrudate through a cooling bath containing a cooling fluid maintained at a temperature of from about 15° C. to about 30° C. such that the drawn extrudate is contacted with the cooling fluid for a period of time of from about 1 to about 30 seconds; (h) drying the drawn extrudate to remove residual cooling fluid therefrom; (i) cutting the dried, drawn extrudate into pellets, said pellets having a bulk density of approximately 36 pounds per cubic foot; (j) airveying the pellets to an upper portion of a cyclone apparatus so the pellets are spirally conveyed downwardly through the cyclone apparatus and cooled to a temperature of less than about 30° C.; (k) discharging the cooled pellets from the cyclone apparatus onto a shaker for removal of particles of matter generated during the cutting of the extrudate into pellets; and (l) discharging the pellets from the shaker into storage bins wherein the pellets are exposed to atmospheric pressure and ambient room temperature for a period of time of at least about 2 hours to permit the vaporizable expanding agent to uniformly disperse through the interior portion of the pellets and provide expandable pellets, said pellets having a bulk density of approximately 36 pounds per cubic foot and expandable upon heating under conditions of maximum volume increase of the pellets so as to provide expanded particles having a bulk density of approximately 0.8 pounds per cubic foot and substantially uniform minute cells having a cell diameter of less than 40 microns formed through an interior portion of the expanded particles.

Claim 17

A process for manufacturing expandable polystyrene pellets comprising: (a) admixing virgin polystyrene beads impregnated with from about 5.9 to about 7.5 weight percent of a vaporizable expanding agent and having a melt index from about 4.5 to 5.0 with from about 0.4 to about 0.25 grams of a nucleating agent per kilogram of polystyrene beads to form an extrusion mixture, said polystyrene beads having a molecule weight within the range of from about 90,000 to about 150,000; (b) introducing the extrusion mixture into an extruder, said extruder characterized as having a melt zone, a cooling zone, a die head and an extruder screw for advancing the extrusion mixture under extrusion pressure towards the die head; (c) heating the extrusion mixture in the melt zone of the extruder to a temperature of from about 115° C. to about 130° C. so as to produce a heat plasticized mass; (d) cooling the heat plasticized mass in the cooling zone of the extruder to a temperature of from about 80° C. to about 100° C. so as to increase the viscosity of the plasticized mass; (e) extruding the cooled plasticized mass into an atmospheric environment through the die head of the extruder at a temperature of from about 115° C. to about 125° C. and at a pressure of from about 1800 psi to about 2200 psi to form an unexpanded extrudate in filamentary form; (f) drawing the extrudate away from said extruder at said temperature of from about 115° C. to about 125° C. and at said pressure of from about 1800 psi to about 2200 psi into the air at a rate of from about 1.5 to about 2.0 times greater than the rate of extrusion to provide a drawn extrudate having a substantially continuous gas impervious skin integral with and covering an interior portion of the drawn extrudate; (g) immediately passing the drawn extrudate through a cooling bath containing a cooling fluid maintained at a temperature of from about 15° C. to about 30° C. such that the drawn extrudate is contacted with the cooling fluid for a period of time of from about 1 to about 30 seconds; (h) drying the drawn extrudate to remove residual cooling fluid therefrom; (i) cutting the dried, drawn extrudate into pellets, said pellets having a bulk density of approximately 36 pounds per cubic foot; (j) airveying the pellets to an upper portion of a cyclone apparatus so the pellets are spirally conveyed downwardly through the cyclone apparatus and cooled to a temperature of less than about 30° C.; (k) discharging the cooled pellets from the cyclone apparatus onto a shaker for removal of particles of matter generated during the cutting of the extrudate into pellets; and (l) discharging the pellets from the shaker into storage bins wherein the pellets are exposed to atmospheric pressure and ambient room temperature for a period of time of at least about 2 hours to permit the vaporizable expanding agent to uniformly disperse through the interior portion of the pellets and provide expandable pellets, said pellets having a bulk density of approximately 36 pounds per cubic foot and expandable upon heating under conditions of maximum volume increase of the pellets so as to provide expanded particles having a bulk density of approximately 0.8 pounds per cubic foot and substantially uniform minute cells having a cell diameter of less than 40 microns formed through an interior portion of the expanded particles.

Claim 18

The process for manufacturing expandable polystyrene pellets of claim 15 wherein the cooling fluid is water and said drawn extrudate is cooled by passing same through a vessel containing said water.

Claim 19

The process of manufacturing expandable polystyrene pellets of claim 15 wherein the vaporizable expanding agent is an aliphatic hydrocarbon.

Claim 20

The process of manufacturing expandable polystyrene pellets of claim 15 wherein the aliphatic hydrocarbon is selected from the group consisting of n-pentane, iso-pentane and mixtures thereof.

Claim 21

The process of manufacturing expandable polystyrene pellets of claim 15 wherein the nucleating agent is selected from the group consisting of amorphous calcium polysilicate and a mixture of citric acid and sodium carbonate.