EP4673295A1

EP4673295A1 - Recovery of vapors and liquids from sheet production process

Info

Publication number: EP4673295A1
Application number: EP24713862.1A
Authority: EP
Inventors: Michael Wandell CRADIC; Michael Eugene Donelson; Steven Thomas Perri; Rebecca Marie GLASPIE
Original assignee: Eastman Chemical Co
Current assignee: Eastman Chemical Co
Priority date: 2023-02-27
Filing date: 2024-02-27
Publication date: 2026-01-07
Also published as: WO2024182329A1

Abstract

Systems and methods for recovering, and optionally recycling, vapor and liquid components produced during a sheet production process. A vapor collection system and/or a liquid collection system is utilized to recover the vapors and liquids that would otherwise be lost or disposed of in traditional sheet production processes and systems. The systems and methods are particularly useful for recovering plasticizer and physical blowing agent components in the production of cellulose ester foam sheets and articles.

Description

RECOVERY OF VAPORS AND LIQUIDS FROM SHEET PRODUCTION PROCESS

BACKGROUND OF THE INVENTION

Many foam articles, such as food-packaging articles, are single-use items that are intended to be disposed of after use. One commercially important material used to make foam articles is polystyrene. However, polystyrene is neither compostable nor biodegradable. Moreover, some municipalities, states, and countries have enacted, or are considering enacting, bans on the use polystyrene-based foams. Thus, it would be desirable to find alternative materials for use in foam articles, as well as viable compositions, methods, and systems for producing such articles.

Additionally, during traditional foam sheet production processes, some quantity of useful vapor and/or liquid is released. Existing processes and systems generally vent or otherwise dispose of such vapor and liquids. For example, various different exhaust systems are currently used that generally exhausted the vapor to a roof vent, and liquid dripping from the systems may be collected in drains for treatment and disposal. Thus, it would be desirable to find alternative systems and methods that recover these vapors and liquid for subsequent use.

SUMMARY OF THE INVENTION

In one embodiment or in combination with any other embodiment mentioned herein, there is provided a method for recovering vapor in a cellulose ester sheet forming process. The method comprises: (a) drying a foamable particulate composition comprising a cellulose ester and a plasticizer, thereby producing a dried particulate material; (b) melting and extruding the dried particulate material through a die head to form an extrudate; (c) processing the extrudate through a sheet forming system; and (d) collecting at least a portion of a vapor produced during the introducing (a), the extruding (b), and/or the processing (c). In another embodiment or in combination with any other embodiment mentioned herein, there is provided a method for recovering a plasticizer in a cellulose ester sheet forming process. The method comprises: (a) introducing a composition comprising a cellulose ester and the plasticizer to an extrusion process; (b) melting and extruding the composition through a die head to form an extrudate; (c) processing the extrudate through a sheet forming system; (d) collecting at least a portion of a plasticizer-containing vapor produced during the introducing (a), the melting and extruding (b) and/or the processing (c) in a vapor collection system; and (e) condensing at least a portion of the plasticizer-containing vapor in the vapor collection system to form a plasticizer-containing liquid.

In another embodiment or in combination with any other embodiment mentioned herein, there is provided a method for recovering an at least partially condensable vapor in a cellulose ester sheet forming process. The method comprises: (a) extruding a composition through an annular die head to form a tubular extrudate; (b) drawing the tubular extrudate over a forming mandrel; (c) slitting the tubular extrudate with a slitting device; and (d) recovering at least a portion of a vapor produced during the extruding (a), the drawing (b), and/or the slitting (c) in a collection system at least partially located adjacent to the die head, the mandrel, and/or the slitting device.

In another embodiment or in combination with any other embodiment mentioned herein, there is provided a method for recycling a plasticizer in a cellulose ester foam sheet forming process. The method comprises: (a) introducing a feed material comprising cellulose ester from a compounding process into an extrusion process; (b) extruding a composition comprising the feed material and a plasticizer through a die head to form an extrudate; (c) processing the extrudate through a sheet forming system; (d) recovering at least a portion of the plasticizer released during the extruding (b) and/or the processing (c); and (e) recycling at least 50 percent by weight of the recovered plasticizer to the compounding process and/or the extrusion process BRIEF DESCRIPTION OF THE DRAWINGS

Figure (FIG.) 1 is a schematic diagram illustrating a biodegradable article forming process according to embodiments of the present invention;

FIG. 2 is a schematic diagram illustrating another biodegradable article forming process according to embodiments of the present invention;

FIG. 3 is a schematic diagram illustrating an extrusion section that may be used in the article forming processes of FIGS. 1 and/or 2, according to embodiments of the present invention;

FIG. 4 is a schematic diagram illustrating another extrusion section that may be used in the article forming process of FIGS. 1 and 2, according to embodiments of the present invention;

FIG. 5 is a schematic diagram illustrating a sheet forming section that may be used in the article forming processes of FIGS. 1 and/or 2, according to embodiments of the present invention;

FIG. 6 is a schematic diagram illustrating an exemplary extrusion section and sheet forming section having an associated vapor collection system and liquid collection system, according to embodiments of the present invention;

FIG. 7 is a schematic diagram illustrating an exemplary vapor collection system and liquid collection system, according to embodiments of the present invention;

FIG. 8 is a schematic diagram illustrating an exemplary vapor inlet associated with a vapor collection system, according to embodiments of the present invention; and

FIG. 9 is a schematic diagram of a volatile recovery system, according to embodiments of the present invention.

DETAILED DESCRIPTION

Embodiments are generally directed to methods, systems, and compositions for forming biodegradable particulate materials (e.g., pellets), foam sheets, and articles. The embodiments described herein are advantageously capable of recovering and, optionally recycling, vapor and liquid components that are released during processing of the materials. Exemplary processes including the methods, systems, and compositions are depicted in FIGS. 1 - 5 and are described in greater detail below.

Methods and Systems

As shown in FIG. 1 and FIG. 2, raw materials may be introduced to a biodegradable polymer production process, which produces a biodegradable polymer material. In one embodiment or in combination with any other embodiment mentioned herein, the biodegradable polymer material comprises one or more cellulose esters. The one or more cellulose esters may comprise cellulose acetates. In such embodiments, the raw materials may comprise a pulp, such as wood pulp and/or cotton pulp. The pulp may be a dissolvinggrade pulp and/or a paper-grade pulp. The cellulose in the pulp may esterified, for example with an acetic acid, to form the biodegradable cellulose ester polymer, such as a cellulose acetate polymer.

The biodegradable polymer material may then be introduced into a compounding process, in which the biodegradable polymer material may be mixed with plasticizer, and optionally one or more other additives (e.g., stabilizers), and formed into a compounded material comprising plasticized biodegradable polymer. Other additives may also be mixed with the polymer and plasticizer. For example, as shown in FIG. 2, the other materials (additives) may include, but are not limited to, stabilizers, physical blowing agent(s), chemical blowing agent(s) (and/or precursors), nucleating agent(s), surface modifying additive(s), pigment(s), filler(s), and/or other additive(s). Mixing can be accomplished by any known mixing technique, including, but not limited to, rolling in a cylindrical container, overhead stirring, sigma blade mixing, and tumbling.

The compounding process may include a particulating process. The particulating process may generally comprise mixing the biodegradable polymer material, plasticizer, and other additive(s) to form a mixed composition and forming particulate material from the composition. In particular, the particulating process may include a pelletization process, and the particulate material may comprise a quantity of pellets. The term “compounded CE material” means cellulose ester material formed during the compounding process, which may include a mixture of cellulose ester, plasticizer, and other additives. Further such compounded CE material may be in the form of particulate material or pellets. It should be understood that, as used herein, the phrases “particulating” or “particu lating processes” may be the same as, or may at least include, “pelletizing” or “pelletizing processes.” In some embodiments, the particulating process may include pelletizing into a water bath, pelletizing on an air cooled belt, underwater pelletizing, solvent compounding, etc.

In one embodiment or in combination with any other embodiment mentioned herein, the plasticizer and other additive(s) may be mixed with cellulose esters by conventional melt compounding techniques, which involve combining the cellulose ester with plasticizer, and optionally the other additives, in a twin screw extruder with appropriate mixing elements and at appropriate temperatures and pressures to achieve a molten, homogeneously combined, cellulose ester mixture by the time the materials exit the extruder. The molten, compounded, cellulose ester mixture may then be extruded through a die with orifices that are about 2-6 mm in diameter so as to extrude a strand. This strand may then be cooled by water (e.g., via underwater pelletization) or air and cut at regular intervals to provide a uniform and desirable size and shape, referred to as “pellets” or “granules.” Although a process for forming pelletized compounded material is described herein, it will be understood that the compounded material fed to the foam sheet production process can be in any physical shape (e.g., pellets, powders, granules, fibers) in accordance with some embodiments. The term “compounded CE material” means cellulose ester material formed during the compounding process, which may include a mixture of cellulose ester, plasticizer, and other additives. Further such compounded CE material may be in the form of a molten mixture or a particulate material (e.g., pellets, powders, granules, fibers, etc.) The compounded CE material, which as noted above may comprise pellets of plasticized biodegradable polymer, may then be optionally dried (see FIG. 6) and introduced into a foam sheet production process, as illustrated in FIGS. 1 and 2. The foam sheet production process may include one or more zones/steps for producing a foam sheet or film, which are described in greater detail below. Although an exemplary foam sheet production process is described herein, it should be understood that certain aspects described herein may also be applicable to rigid (i.e., non-foamed) materials and articles. As shown in FIG. 1 , in one embodiment or in combination with any other embodiment mentioned herein, various additives may be introduced to one or more zones of the foam sheet production process. The additives may include, but are not limited to, stabilizers, physical blowing agent(s), chemical blowing agent(s) (and/or precursors), nucleating agent(s), surface modifying additive(s), pigment(s), filler(s), and/or other additive(s).

The foam sheet production process may generally include an extrusion section and a sheet forming section. An exemplary extrusion section is depicted in FIG. 3. As shown, the extrusion section may comprise a feed preparation zone, in which solid additives may be combined with the compounded CE material and introduced to the downstream extrusion zone. In one embodiment or in combination with any other embodiment mentioned herein, the feed preparation zone may comprise a feed hopper. Thus, the compounded CE material and the other solid additives may be deposited into the feed hopper, which directs the combined feed composition into the extrusion zone. The feed preparation zone may further comprise a mixer, in which the compounded CE material and one or more additive(s) may be mixed before being introduced to the hopper. Mixing can be accomplished by any known mixing technique, including, but not limited to, rolling in a cylindrical container, overhead stirring, sigma blade mixing, and tumbling. Exemplary solid additive(s) that can be combined with the compounded material may include chemical blowing agent(s), nucleating agent(s), surface modifying additive(s), pigment(s), filler(s), and/or other additive(s). The combined feed composition from the feed preparation zone may then be introduction to the extrusion zone. The extrusion zone may generally comprise one or more extruders, which may include single screw and/or twin screw extruders. Within the extruder(s), the feed composition may be introduced into an extruder barrel and conveyed, via the screw(s), through a die, which forms an extrudate from the feed composition. The composition may be heated, and at least partially melted, as it is conveyed through the extruder barrel toward the die. Thus, the term “CE melt composition” is used herein to mean the cellulose ester-based feed composition that has been melted into a flowable, molten resin via the extrusion section. Heating may be supplied by external heaters positioned along the outside of the extruder barrel. The shape of the extrudate will generally depend on the shape and size of the die head. The extrudate may be further shaped by downstream processes, as described below.

One or more additive(s) may be introduced to the CE melt composition while in the extruder. For example, one or more physical blowing agent(s) may be added to the CE melt composition by injecting the physical blowing agent into the composition being conveyed within the extruder barrel.

As depicted in FIG. 4, in one embodiment or in combination with any other embodiment mentioned herein, the extrusion zone may comprise a primary extrusion vessel and a cooling vessel. The primary extrusion vessel and cooling vessel may be separate devices or combined as a unitary apparatus. Regardless, the feed composition from the feed preparation zone is introduced into the primary extrusion vessel and at least partially melted as it is conveyed through the extruder barrel, as described above, to thereby produce the CE melt composition. The CE melt composition exiting the primary extrusion vessel may have a temperature from about 220° C to about 240° C. One or more additives, such as blowing agent(s), may be added to the CE melt composition as it is conveyed through the primary extrusion vessel.

The CE melt composition from the primary extrusion vessel is then introduced into the cooling vessel. The cooling vessel may be a secondary extrusion vessel, which operates similarly to, but at a lower temperature than, the primary extrusion vessel. Within the cooling vessel, the CE melt composition may be further mixed to provide a substantially homogenous mixture of the melted polymer and other additive(s). The CE melt composition may then be directed through the die and out of the die head to provide a cellulose ester-based extrudate, which may be further processed in the sheet forming section of the foam sheet production process. In one embodiment or in combination with any other embodiment mentioned herein, the CE melt composition exiting the die head may have a temperature of at least 150° C, at least 160° C, at least 170° C, at least 180° C, at least 190° C, at least 200° C, from about 150° C to about 220° C, and/or from about 170° C to about 200° C.

As shown in FIG. 4, one or more filtration devices may be installed within the extrusion section to filter and remove particulate matter from the CE melt composition. For example, screen changer filtration devices may be installed at the downstream end of the primary and secondary extrusion vessels, which may remove solid components from the CE melt composition before directing the CE melt compositions through the die head to the sheet forming section.

The sheet forming section may include any of a variety of systems and processes for shaping the extrudate into sheets of cellulose ester material that may be used in article formation. The shape of the extrudate will generally depend on the shape of the die head, while the shape of the sheets formed in the sheet forming section can depend on the shape of the die head and other downstream processes. For example, the extrudate may have a generally flat shape, or it may be annular and subjected to further processing to form a flat sheet. In embodiments in which the die has an annular shape, the die may have a diameter from 1 to 40 cm, from 2 to 20 cm, 2 to 10 cm, and/or 3 to 8 cm. Furthermore, the thickness of the opening from which extrudate is ejected, which is referred to herein as a “die gap,” may generally be sized from 0.1 to 6.0 mm, from 0.1 to 3.0 mm, and/or from 0.1 to 1.0 mm. An exemplary sheet forming section is depicted in FIG. 5. As shown, the CE melt composition is extruded through an annular die and drawn over a forming mandrel. A cooling fluid (e.g., air) may be flowed across the interior and/or exterior of the extrudate to cool the extrudate material as it passes over the mandrel. For example, the cooling fluid may be blown from the mandrel toward the die to cool the interior surface of the extrudate between the die and mandrel. Additionally or alternatively, the cooling fluid may be flowed across the mandrel to cool the exterior surface of the extrudate as it passes over the mandrel.

A slicer (or slitting device) may be used to open the tubular extrudate, which allows the tubular shape to be formed into a flat sheet. For example, the tubular extrudate passing over the mandrel may be slit and drawn to a tensioning station comprising one or more rollers that flatten the extrudate and maintain a necessary amount of tension on the extrudate to continue pulling the extrudate over the mandrel. The flattened extrudate will generally be in the form of a sheet, which may then be directed to a winding station where the material may be rolled for packaging and transportation.

Referring again to FIG. 1 and FIG. 2, the sheets produced by the sheet production process may be used to form foam articles, which are described in greater detail below. Such articles are particularly useful in the food service industry. Exemplary articles include meat trays. The articles may have one or more particularly advantageous properties. For example, the articles may be biodegradable and/or compostable, and/or the articles may have superior mechanical properties (e.g., strength, density, cell size, absorption, etc.).

During one or more of the operations described above, some quantity of useful vapor and/or liquid may be released from the CE material being processed. When the CE material is plasticized with a plasticizer that is volatile during the extrusion process, the vapor will be plasticizer-containing with a plasticizer component. Other components of the CE material can be present in the vapor. For example, valuable plasticizer and/or physical blowing agent in the compounded material, the melt composition, and/or the extrudate may be vaporized during processing. Additionally or alternatively, valuable plasticizer may separate as a condensate liquid on the extrudate. In one embodiment or in combination with any other embodiment mentioned herein, at least a portion of the vapors and/or liquids produced during these operations may be recovered for further use.

Referring now to FIG. 6, a sheet forming process is illustrated, which may include any one or more of the operations described above with respect to FIGS. 1 - 5, as well as systems for recovering vapors and liquids produced during such operations.

As shown in FIG. 6, the biodegradable polymer materials may be introduced to a compounding process, as described above to form a particulate feed composition to the extrusion section. In one embodiment or in combination with any other embodiment mentioned herein, the particulate composition may be dried to produce a dried particulate material before being introduced to the extrusion section (e.g., via a feed zone hopper). During the drying, vapor removed from the particulate material may include plasticizer and/or physical blowing agent along with water. At least a portion of this vapor may be recovered in the vapor collection system and may be used elsewhere in the sheet forming process.

In one embodiment or in combination with any other embodiment mentioned herein, at least a portion of the particulate CE material produced in the compounding process may be dried by introducing the material into a drying system to reduce the moisture content and thereby provide a dried particulate material. In the drying system, the particulate CE material may be contacted with a forced vapor (e.g., air) stream passed through the drying system and over/through the particulate material. The vapor stream may comprise compressed dry air, which may be introduced at a temperature and humidity sufficient to draw out water from the composition. The drying temperature (i.e., the temperature of the vapor stream) may be at least 60 °C below the Tg of the CE material. Thus, the forced vapor stream may have a temperature of 40 °C to 80 °C, or 50 °C to 70 °C. In some embodiments, the forced vapor stream may be cooled and contacted with a desiccant material. Cooling the gaseous stream before contact with the desiccant material may advantageously condense certain volatiles (for collection and/or reuse) and can make the desiccant operate more efficient. Additionally, or alternatively, other drying methods may also be used, which may include one or more heating steps, air drying, and/or cyclone drying processes.

In one embodiment or in combination with any other embodiment mentioned herein, the forced vapor stream used in the drying system may be processed to remove (and optionally collect) volatiles and/or particulate matter (e.g., dust, fines, etc.) becoming entrained therein, which allows the processed vapor stream to be recirculated for use in the drying system. An exemplary system for processing the vapor stream is depicted in FIG. 9. The vapor stream is fed through an inlet, where it may be optionally first subjected to particulate filtration to remove dust and other fine particulate matter. The vapor stream at the inlet may have a temperature of 40 °C to 80 °C, or 50 °C to 70 °C. The (optionally filtered) vapor stream is then cooled and at least partially condensed. For example, the vapor stream may be passed over a cooling coil, or other heat exchanger, thereby condensing at least a portion of the volatile components from the vapor stream. The vapor stream and any condensed liquid can then be passed to a condensate collection zone, which may include one or more steps operable to remove the condensate from the vapor stream. For example, a first step may include contacting the vapor stream with baffles or other surfaces, upon which the condensate may form and flow downward into a catch basin positioned at the bottom of the processing system. Other steps may include redirection (e.g., upward) and velocity change of the vapor stream, which can cause at least a portion of the entrained condensate to separate from the vapor stream and fall for collection and recovery in the catch basin. Additionally, or alternatively, a second cooling step may be utilized to further condense at least a portion of the volatile components remaining in the vapor stream. For example, in some embodiments, the first cooling step may condense 50-80% of the volatile components in the vapor stream, while the second cooling step may condense 20-50% of the volatile components in the vapor stream. Finally, the vapor stream may be optionally subjected to further filtration, including particulate filtration and/or scrubbing filtration to recovery any remaining condensate in the vapor stream before the vapor stream is directed through the outlet. The temperature of the vapor stream exiting the system may be 0 °C to 10 °C lower, or 1 °C to 5 °C lower than the temperature of the vapor stream at the inlet. In some embodiments, the recovered condensate can be optionally filtered and stored or recycled for further use. For example, in some embodiments, the condensate comprises a blowing agent and/or plasticizer that was volatilized during drying, and the condensed blowing agent and/or plasticizer can be recycled back for use in the compounding process described above.

Referring again to FIG. 6, the (optionally dried) particulate material is then melted and extruded in the extrusion section. During the melting and extruding processes, vapor may be produced from the heated melt composition, which may include plasticizer and/or physical blowing agent. At least a portion of this vapor may be recovered in the vapor collection and may be used elsewhere in the sheet forming process.

The extrudate from the extrusion process is then processed in a sheet forming section, such as described herein. For example, as shown in FIG. 5 and FIG. 7, the melt composition may be extruded through an annular die, and the tubular extrudate drawn over a forming mandrel, whereby the extrudate begins to cool. The tubular extrudate may be slit (e.g., via a slicer or slitter) and wound into sheets. During one or more of these processes, vapor may be produced from the extrudate, which may include plasticizer and/or physical blowing agent. At least a portion of this vapor may be recovered in the vapor collection and may be used elsewhere in the sheet forming process. Additionally, or alternatively, a liquid condensate may form on the extrudate, which may similarly be recovered and used elsewhere in the sheet forming process.

Referring now to FIG. 7, exemplary vapor collection and liquid collection systems are illustrated. As shown, the vapor collection system may be located adjacent one or more (or at least two) of the extrusion barrel, the extrusion die head, the forming mandrel, and/or the slitting device. For example, the vapor collection system may comprise one or more vapor collection conduits (e.g., ducts) having an inlet at least partially positioned above the annular die and/or the mandrel. The inlet may be, for example, a single large hood or multiple smaller hoods positioned above the annular die and/or mandrel. In one embodiment or in combination with any other embodiment mentioned herein, the inlet(s) may be positioned less than 5 feet, less than 4 feet, less than 3 feet, less than 2 feet, or less than 1 foot above the annular die and/or the mandrel. Vapor may be recovered by suctioning (e.g., pump, vacuum, etc.) at least a portion of the vapor through the inlet and directing the vapor to a condensation unit in the vapor collection system. In some embodiments, a structure that channels (e.g., a tube, a guard, a curtain, or a chimney like structure) the vapors from the extrusion process to the inlet may be used. In some embodiments, the condensation unit may comprise a condensation trap (e.g., comprising a cooling radiator) or other condenser. The condensation unit may be disposed in the vapor collection conduit(s) so as to cool and at least partially condense the condensable components directed through the conduit(s). Additionally, or alternatively, the condensation unit may comprise a volatiles collection system, such as shown in FIG. 9 and described above.

In one embodiment or in combination with any other embodiment mentioned herein, the recovered vapor may include one or more condensable components and one or more non-condensable components. Exemplary condensable components may include plasticizers as described herein, as well as vaporized water (H2O), acids (e.g., acetic acid), phosphites, coblowing agent (e.g., ketones, alcohols), and/or oils (e.g., epoxidized soybean oil). For example, the recovered vapor may comprise at least 50 percent, at least 60 percent, at least 70 percent, at least 80 percent, or at least 90 percent by weight of plasticizer, based on total weight of vapor taken as 100 percent by weight. Exemplary non-condensable components may include physical blowing agents (e.g., carbon dioxide, hydrocarbons), as described herein. The weight ratio of condensable to non-condensable components in the recovered vapor may be 1 :1 to 100:1 , or 5:1 to 50:1 , or 10:1 to 20:1 . In one embodiment or in combination with any other embodiment mentioned herein, the vapor collection system can recover 0.1% to 5%, 0.2 to 4%, 0.3 to 3%, 0.4 to 2%, or 0.5% to 1% by weight of the plasticizer present in the particulate material (i.e. , the portion of the plasticizer that volatilizes during drying, heating, melting, extruding, and/or drawing the material). In operation, the vapor collection system can recover 0.1 gal/hour to 5 gal/hour, or 0.5 gal/hour to 2 gal/hour (or 100 Ib/hour to 5000 Ib/hour, or 500 Ib/hour to 2000 Ib/hour) of plasticizer.

In one embodiment or in combination with any other embodiment mentioned herein, at least a portion of the recovered vapor may be condensed to form a liquid, which can be recovered and/or recycled to the melt composition in the extruder or other upstream process described herein. For example, the condensed liquid may comprise a plasticizer that can be recycled to the compositions in the compounding and/or extrusion processes. In some embodiments, at least 50, at least 60, at least 70, at least 80, at least 90, or at least 95 percent by weight of a recovered plasticizer is recycled to the compounding process and/or to the extrusion process. In some embodiments, the plasticizer may be dripped into the composition (e.g., in a twin screw extruder barrel, in the feed zone) or injected into the composition (e.g., in a single screw extruder barrel).

Additionally, or alternatively, at least a portion of the recovered vapor may comprise non-condensable component(s) that are separated from the condensable components in the condenser. The non-condensable component(s) can then be recovered and/or recycled to the melt composition in the extruder or other upstream process described herein. For example, the non-condensable component(s) may comprise a physical blowing agent that can be introduced to the composition in the extrusion process.

In one embodiment or in combination with any other embodiment mentioned herein, the recovered vapor may be filtered to remove particulates entrained in the vapor before or after the condensing step. The filtering may be accomplished by utilizing an electrostatic precipitation process. In some embodiments, a first filtration step may occur upstream of the condensing step to remove coarse particles (e.g., at least 0.8 mm, at least 1 .0 mm, at least 1 .5 mm, or at least 2.0 mm particle size), and a second filtration step may occur downstream of the condensing step to remove fine particulates (less than 2.0 mm, less than 1 .5 mm, less than 1 .0 mm, or less than 0.8 mm particle size).

In one embodiment or in combination with any other embodiment mentioned herein, the vapor collection system may comprise a volatile recovery system and process, including one or more filtration and/or one or more condensation steps, such as depicted in FIG. 9 and described in greater detail above.

In one embodiment or in combination with any other embodiment mentioned herein, a spout may be positioned downstream of the mandrel and operable to collect liquid condensate formed on the mandrel and/or extrudate. The collected liquid may comprise a plasticizer and may be combined with other condensed liquids recovered and/or recycled to upstream processes, as described herein.

Referring now to FIG. 8, an exemplary vapor inlet is illustrated. As shown, the vapor inlet may comprise a lip defining a perimeter channel around the inlet opening. During suctioning of the vapor, at least a portion of the vapor may condense on the inner surfaces of the inlet and conduit. One or more baffles may be disposed within the inlet to provide for additional surfaces for the vapor to condense upon. The baffles may be angled upward (e.g., 45 degrees) so as to allow the vapor to flow upward while still providing additional condensation surfaces. This condensate may flow down the interior surface of the inlet and be collected in the channel. The liquid condensate may then be drained from the channel and recovered. At least a portion of the liquid condensate may then be combined with one or more other liquids recovered in the vapor collection system and/or the liquid collection system and optionally recycled as described herein. Compositions

The processes described above may comprise the preparation and extrusion of compositions that may be used for downstream processing to form useful articles. For example, in one embodiment or in combination with any other embodiment mentioned herein, the extrusion feed material may comprise a particulate material comprising a biodegradable polymer, a plasticizer, and optionally one or more additive(s), such as those described herein. In one embodiment or in combination with any other embodiment mentioned herein, the feed material may be combined with one or more additive(s), such as those described herein, to provide a mixed composition comprising the biodegradable polymer, the plasticizer, and the one or more additive(s). In one embodiment or in combination with any other embodiment mentioned herein, the biodegradable polymer comprises cellulose ester. Additional details of the composition components, including biodegradable polymers (e.g., cellulose esters), plasticizers, and other additives, are provided below.

Cellulose Ester

The cellulose esters utilized as described herein can be any that is known in the art. Cellulose ester that can be used for embodiments herein generally comprise repeating units of the structure:

1 2 2 wherein R , R , and R are selected independently from the group consisting of hydrogen acetyl, propyl or butyl. The substitution level of the cellulose ester is usually expressed in terms of degree of substitution (DS), which is the average number of non-OH substituents per anhydroglucose unit (AGU). Generally, conventional cellulose contains three hydroxyl groups in each AGU unit that can be substituted; therefore, DS can have a value between zero and three. Native cellulose is a large polysaccharide with a degree of polymerization from 250 - 5,000 even after pulping and purification, and thus the assumption that the maximum DS is 3.0 is approximately correct. Because DS is a statistical mean value, a value of 1 does not assure that every AGU has a single substitutent. In some cases, there can be unsubstituted anhydroglucose units, some with two and some with three substitutents, and typically the value will be a non-integer. Total DS is defined as the average number of all of substituents per anhydroglucose unit. The degree of substitution per AGU can also refer to a particular substitutent, such as, for example, hydroxyl or acetyl. In one embodiment or in combination with any other embodiment, n is an integer in a range from 25 to 250, or 25 to 200, or 25 to 150, or 25 to 100, or 25 to 75.

In one embodiment or in combination with any other embodiment, the cellulose esters have at least 2 anhydroglucose rings and can have between at least 50 and up to 5,000 anhydroglucose rings, or at least 50 and less than 150 anhydroglucose rings. The number of anhydroglucose units per molecule is defined as the degree of polymerization (DP) of the cellulose ester. In one embodiment or in combination with any other embodiment, cellulose esters can have an inherent viscosity (IV) of about 0.2 to about 3.0 deciliters/gram, or about 0.5 to about 1 .8, or about 1 to about 1 .5, as measured at a temperature of 25°C for a 0.25 gram sample in 100 ml of a 60/40 by weight solution of phenol/tetrachloroethane. In one embodiment or in combination with any other embodiment, cellulose esters useful herein can have a DS/ AGU of about 1 to about 3.0, or of about 2.0 to about 2.9, or of about 2.2 to about 2.8, or 1 to less than 2.2, or 1 to less than 1 .5, and the substituting ester is acetyl.

Cellulose esters can be produced by any method known in the art. Examples of processes for producing cellulose esters are taught in Kirk- Othmer, Encyclopedia of Chemical Technology, 5th Edition, Vol. 5, Wiley- Interscience, New York (2004), pp. 394-444. Cellulose, the starting material for producing cellulose esters, can be obtained in different grades and sources such as from cotton linters, softwood pulp, hardwood pulp, corn fiber and other agricultural sources, and bacterial cellulose, among others.

One method of producing cellulose esters is esterification of the cellulose by mixing cellulose with the appropriate organic acids, acid anhydrides, and catalysts. Cellulose is then converted to a cellulose triester. Ester hydrolysis is then performed by adding a water-acid mixture to the cellulose triester, which can then be filtered to remove any gel particles or fibers. Water is then added to the mixture to precipitate the cellulose ester. The cellulose ester can then be washed with water to remove reaction byproducts followed by dewatering and drying.

The cellulose triesters to be hydrolyzed can have three acetyl substituents. These cellulose esters can be prepared by a number of methods known to those skilled in the art. For example, cellulose esters can be prepared by heterogeneous acylation of cellulose in a mixture of carboxylic acid and anhydride in the presence of a catalyst such as H2SO4. Cellulose triesters can also be prepared by the homogeneous acylation of cellulose dissolved in an appropriate solvent such as LiCI/DMAc or LiCI/NMP.

Those skilled in the art will understand that the commercial term of cellulose triesters also encompasses cellulose esters that are not completely substituted with acyl groups. For example, cellulose triacetate commercially available from Eastman Chemical Company, Kingsport, TN, U.S.A., typically has a DS from about 2.85 to about 2.99.

After esterification of the cellulose to the triester, part of the acyl substituents can be removed by hydrolysis or by alcoholysis to give a secondary cellulose ester. As noted previously, depending on the particular method employed, the distribution of the acyl substituents can be random or non-random. Secondary cellulose esters can also be prepared directly with no hydrolysis by using a limiting amount of acylating reagent. This process is particularly useful when the reaction is conducted in a solvent that will dissolve cellulose. All of these methods yield cellulose esters that are useful in this invention. In one embodiment or in combination with any of the mentioned embodiments, the cellulose acetates are cellulose diacetates that have a polystyrene equivalent number average molecular weight (Mn) from about 10,000 to about 100,000 as measured by gel permeation chromatography (GPC) using NMP as solvent and polystyrene equivalent Mn according to ASTM D6474. In one embodiment or in combination with any other embodiment, the cellulose acetate composition comprises cellulose diacetate having a polystyrene equivalent number average molecular weights (Mn) from 10,000 to 90,000; or 10,000 to 80,000; or 10,000 to 70,000; or 10,000 to 60,000; or 10,000 to less than 60,000; or 10,000 to less than 55,000; or 10,000 to 50,000; or 10,000 to less than 50,000; or 10,000 to less than 45,000; or 10,000 to 40,000; or 10,000 to 30,000; or 20,000 to less than 60,000; or 20,000 to less than 55,000; or 20,000 to 50,000; or 20,000 to less than 50,000; or 20,000 to less than 45,000; or 20,000 to 40,000; or 20,000 to 35,000; or 20,000 to 30,000; or 30,000 to less than 60,000; or 30,000 to less than 55,000; or 30,000 to 50,000; or 30,000 to less than 50,000; or 30,000 to less than 45,000; or 30,000 to 40,000; or 30,000 to 35,000; as measured by gel permeation chromatography (GPC) using NMP as solvent and according to ASTM D6474.

The most common commercial secondary cellulose esters are prepared by initial acid catalyzed heterogeneous acylation of cellulose to form the cellulose triester. After a homogeneous solution in the corresponding carboxylic acid of the cellulose triester is obtained, the cellulose triester is then subjected to hydrolysis until the desired degree of substitution is obtained. After isolation, a random secondary cellulose ester is obtained. That is, the relative degree of substitution (RDS) at each hydroxyl is roughly equal.

The cellulose esters useful in the present invention can be prepared using techniques known in the art, and can be chosen from various types of cellulose esters, such as for example the cellulose esters that can be obtained from Eastman Chemical Company, Kingsport, TN, U.S.A., e.g., Eastman™ Cellulose Acetate CA 398-30 and Eastman™ Cellulose Acetate CA 398-10, Eastman™ CAP 485-20 cellulose acetate propionate; Eastman™ CAB 381-2 cellulose acetate butyrate.

In one embodiment or in combination with any other embodiment, the cellulose ester can be prepared by converting cellulose to a cellulose ester with reactants that are obtained from recycled materials, e.g., a recycled plastic content syngas source. In one embodiment or in combination with any other embodiment, such reactants can be cellulose reactants that include organic acids and/or acid anhydrides used in the esterification or acylation reactions of the cellulose, e.g., as discussed herein.

In one embodiment or in combination with any of the mentioned embodiments, or in combination with any of the mentioned embodiments, of the invention, a cellulose ester composition comprising at least one recycle cellulose ester is provided, wherein the cellulose ester has at least one substituent on an anhydroglucose unit (AU) derived from recycled content material, e.g., recycled plastic content syngas.

In one embodiment or in combination with any other embodiment, the cellulose ester composition comprises cellulose ester in an amount from 50 to 99 wt%, or 60 to 99 wt%, or 70 to 99 wt%, or 80 to 99 wt%, from 50 to 98 wt%, or 60 to 98 wt%, or 70 to 98 wt%, or 80 to 98 wt%,or 90 to 98 wt%, 50 to 90 wt%, or 60 to 90 wt%, or 70 to 90 wt%, or 80 to 90 wt%, or 90 to 99 wt%, or 50 to 80 wt%, or 60 to 80 wt%, or 70 to 80 wt%, or 50 to 70 wt%, or 60 to 70 wt%, or 50 to 60 wt%, all based on the total weight of the cellulose ester composition. In some embodiments, the cellulose ester used herein may comprise a combination, blend, or mixture of two or more different types of cellulose esters. For example, in some embodiments, the cellulose esters used herein may be comprised of a blend of two or cellulose esters having differing DSACs; however, the blend may have an total DSAC of between 2.2 and 2.8 or of between 2.0 and 2.9.

Plasticizer

In one embodiment or in combination with any other embodiment, the cellulose ester compositions described herein can comprise at least one plasticizer. The plasticizer reduces the melt temperature, i.e., the Tg, and/or the melt viscosity of the cellulose ester. Plasticizers for cellulose esters may include glycerol triacetate (Triacetin), glycerol diacetate (Diacetin), dibutyl terephthalate, dimethyl phthalate, diethyl phthalate, polyethylene glycol) MW 200-600, dibutyl tartrate, di-2-methoxyethyl phthalate, ethyl o- benzoylbenzoate, triethylene glycol dipropionate, 1 ,2-epoxypropylphenyl ethylene glycol, 1 ,2-epoxypropyl(m-cresyl) ethylene glycol, 1 ,2-epoxypropyl(o- cresyl) ethylene glycol, p-oxyethyl cyclohexenecarboxylate, bis(cyclohexanate) diethylene glycol, triethyl citrate, polyethylene glycol, propylene glycol, polysorbate, sucrose octaacetate, acetylated triethyl citrate, acetyl tributyl citrate, Admex, tripropionin, Scandiflex, poloxamer copolymers, polyethylene glycol succinate, diisobutyl adipate, polyvinyl pyrollidone, and glycol tribenzoate, the benzoate containing plasticizers such as the Benzoflex™ plasticizer series, poly (alkyl succinates) such as poly (butyl succinate), polyethersulfones, o-Cresyl p-toluenesulfonate, n- ethyltoluenesulfonamides, adipate based plasticizers, soybean oil epoxides such as the Paraplex™ plasticizer series, sucrose based plasticizers, dibutyl sebacate, tributyrin, sucrose acetate isobutyrate, the Resolflex™ series of plasticizers, triphenyl phosphate (TPP), triethyl phosphate (TEP), glycolates (e.g., ethyl phthalyl ethyl glycolate “EPEG” and methyl phthalyl ethyl glycolate “MPEG”), methoxy polyethylene glycol, 2,2,4-trimethylpentane-1 ,3-diyl bis(2- methylpropanoate), and polycapro lactones. In some embodiments, the plasticizer used herein may comprise a combination or mixture of two or more different types of plasticizers.

In one embodiment or in combination with any other embodiment, has a boiling point of at least 100 °C, or at least 200 °C, and/or not more than 400 °C, or not more than 300 °C.

In one embodiment or in combination with any other embodiment, the plasticizer is a food-compliant plasticizer. By food-compliant is meant compliant with applicable food additive and/or food contact regulations where the plasticizer is cleared for use or recognized as safe by at least one (national or regional) food safety regulatory agency (or organization), for example listed in the 21 CFR Food Additive Regulations or otherwise Generally Recognized as Safe (GRAS) by the US FDA. In one embodiment or in combination with any other embodiment, the food-compliant plasticizer is triacetin or polyethylene glycol (PEG) having a molecular weight of about 200 to about 600. In one embodiment or in combination with any other embodiment, examples of food-compliant plasticizers that could be considered can include triacetin, triethyl citrate, polyethylene glycol, Benzoflex, propylene glycol, polysorbate, sucrose octaacetate, acetylated triethyl citrate, acetyl tributyl citrate, Admex, tripropionin, Scandiflex, poloxamer copolymers, polyethylene glycol succinate, diisobutyl adipate, polyvinyl pyrollidone, and glycol tribenzoate.

In one embodiment or in combination with any other embodiment, the plasticizer can be present in an amount sufficient to permit the cellulose ester composition to be melt processed (or thermally formed) into useful articles, e.g., single use plastic articles, in conventional melt processing equipment. In one embodiment or in combination with any other embodiment, the plasticizer is present in an amount from 1 to 40 wt% for most thermoplastics processing; or 5 to 25 wt%, or 10 to 25 wt%, or 12 to 20 wt% based on the weight of the cellulose ester composition. In one embodiment or in combination with any other embodiment, profile extrusion, sheet extrusion, thermoforming, and injection molding can be accomplished with plasticizer levels in the 10-30, or 12-25, or 15-20, or 10-25 wt% range, based on the weight of the cellulose ester composition.

In one embodiment or in combination with any other embodiment, the plasticizer is a biodegradable plasticizer. Some examples of biodegradable plasticizers include triacetin, triethyl citrate, acetyl triethyl citrate, polyethylene glycol, the benzoate containing plasticizers such as the Benzoflex™ plasticizer series, poly (alkyl succinates) such as poly (butyl succinate), polyethersulfones, adipate based plasticizers, soybean oil epoxides such as the Paraplex™ plasticizer series, sucrose based plasticizers, dibutyl sebacate, tributyrin, the Resoflex™ series of plasticizers, triphenyl phosphate, glycolates, polyethylene glycol, 2,2,4-trimethylpentane-1 ,3-diyl bis(2- methylpropanoate), and polycapro lactones.

In one embodiment or in combination with any other embodiment, the cellulose ester composition can contain a plasticizer selected from the group consisting of PEG and MPEG (methoxy PEG). The polyethylene glycol or a methoxy polyethylene glycol composition having an average molecular weight of from 200 Daltons to 600 Daltons, wherein the composition is melt processable, biodegradable, and disintegrable.

In one embodiment or in combination with any other embodiment, the composition comprises polyethylene glycol or methoxy PEG having an average molecular weight of from 300 to 550 Daltons.

In one embodiment or in combination with any other embodiment, the composition comprises polyethylene glycol having an average molecular weight of from 300 to 500 Daltons.

In one embodiment or in combination with any other embodiment, the cellulose ester composition comprises at least one plasticizer (as described herein) in an amount from 1 to 40 wt%, or 5 to 40 wt%, or 10 to 40 wt%, or 12 to 40 wt%, 13 to 40 wt%, or 15 to 40 wt%, or greater than 15 to 40 wt%, or 17 to 40 wt%, or 20 to 40 wt%, or 25 to 40 wt%, or 5 to 35 wt%, or 10 to 35 wt%, or 13 to 35 wt%, or 15 to 35 wt%, or greater than 15 to 35 wt%, or 17 to 35 wt%, or 20 to 35 wt%, or 5 to 30 wt%, or 10 to 30 wt%, or 13 to 30 wt%, or 15 to 30 wt%, or greater than 15 to 30 wt%, or 17 to 30 wt%, or 5 to 25 wt%, or 10 to 25 wt%, or 13 to 25 wt%, or 15 to 25 wt%, or greater than 15 to 25 wt%, or 17 to 25 wt%, or 5 to 20 wt%, or 10 to 20 wt%, or 13 to 20 wt%, or 15 to 20 wt%, or greater than 15 to 20 wt%, or 17 to 20 wt%, or 5 to 17 wt%, or 10 to 17 wt%, or 13 to 17 wt%, or 15 to 17 wt%, or greater than 15 to 17 wt%, or 5 to less than 17 wt%, or 10 to less than 17 wt%, or 13 to less than 17 wt%, or 15 to less than 17 wt%, all based on the total weight of the cellulose ester composition.

In one embodiment or in combination with any other embodiment, the at least one plasticizer includes or is a food-compliant or FDA approved plasticizer. In one embodiment or in combination with any other embodiment, the food-compliant or FDA approved plasticizer includes or is triacetin or PEG MW 300 to 500.

Biodegradable Polymers

In one embodiment or in combination with any other embodiment, the cellulose ester compositions described herein comprise a biodegradable cellulose ester (BCE) component that comprises at least one BCE, which may include one or more of the cellulose esters described herein, and a biodegradable polymer component that comprises at least one other biodegradable polymer (other than the BCE). In one embodiment or in combination with any other embodiment, the other biodegradable polymer can be chosen from polyhydroxyalkanoates (PHAs and PHBs), polylactic acid (PLA), polycaprolactone polymers (PCL), polybutylene adipate terephthalate (PBAT), polyethylene succinate (PES), polyvinyl acetates (PVAs), polybutylene succinate (PBS) and copolymers (such as polybutylene succinate-co-adipate (PBSA)), cellulose esters, cellulose ethers, starch, proteins, derivatives thereof, and combinations thereof. In one embodiment or in combination with any other embodiment, the cellulose ester composition comprises two or more biodegradable polymers. In one embodiment or in combination with any other embodiment, the cellulose ester composition contains a biodegradable polymer (other than the BCE) in an amount from 0.1 to less than 50 wt%, or 1 to 40 wt%, or 1 to 30 wt%, or 1 to 25 wt%, or 1 to 20 wt%, based on the cellulose ester composition. In one embodiment or in combination with any other embodiment, the cellulose ester composition contains a biodegradable polymer (other than the BCE) in an amount from 0.1 to less than 50 wt%, or 1 to 40 wt%, or 1 to 30 wt%, or 1 to 25 wt%, or 1 to 20 wt%, based on the total amount of BCE and biodegradable polymer. In one embodiment or in combination with any other embodiment, the at least one biodegradable polymer comprises a PHA having a weight average molecular weight (Mw) in a range from 10,000 to 1 ,000,000, or 50,000 to 1 ,000,000, or 100,000 to 1 ,000,000, or 250,000 to 1 ,000,000, or 500,000 to 1 ,000,000, or 600,000 to 1 ,000,000, or 600,000 to 900,000, or 700,000 to 800,000, or 10,000 to 500,000, or 10,000 to 250,000, or 10,000 to 100,000, or 10,000 to 50,000, measured using gel permeation chromatography (GPC) with a refractive index detector and polystyrene standards employing a solvent of methylene chloride. In one embodiment or in combination with any other embodiment, the PHA can include a polyhydroxybutyrate-co- hydroxyhexanoate.

Nucleating Agent

Nucleating agent means a chemical or physical material that provides sites for cells to form in a molten formulation mixture, such as within a CE melt composition. As will be described in more detail below, nucleating agents may be added to compounded CE material during the compounding process. Alternatively, or in addition, nucleating agents may be added during the foam sheet production process. For example, the nucleating agents may be blended with the formulation that is introduced into the hopper of the extruder of the extruding section. Alternatively, the nucleating agents may be added to the CE melt composition in the extruder itself. Nucleating agents may include physical nucleating agents and chemical nucleating agents. Physical nucleating agents are materials that are immiscible with the polymer matrix of the CE melt composition at the extrusion temperature of the extrusion section. Chemical nucleating agents are materials that react (e.g., decompose) during extrusion (e.g., at the extrusion temperature within the extruder) to form physical nucleating agents. Thus, chemical nucleating agents may be considered (and referred to herein as) precursors of in situ formed physical nucleating agents.

Suitable physical nucleating agents will comprise fine particles having desirable particle sizes and/or shapes to create cell nucleation sites within the CE melt composition. For example, in some embodiments, physical nucleating agents will have a mean particle size of less than 1000 microns, less than 500 microns, less than 100 microns, less than 50 microns, less than 25 microns, less than 20 microns, less than 10 microns, less than 5 microns, less than 2 microns, less than 1 .5 microns, and/or less than 1 .0 microns. However, in some other embodiments, it may be preferred to have nanoscalesized particles. Furthermore, it some embodiments, physical nucleating agents will preferably have a high aspect ratio (i.e., width :height). For example, in some embodiments, physical nucleating agents will have a mean aspect ratio of greater than 1 :1 , greater than 2:1 , greater than 5:1 , greater than 10:1 , greater than 20:1 , greater than 30:1 , greater than 40:1 , greater than 50:1 , greater than 75:1 , and/or greater than 100:1 . Furthermore still, as noted above, physical nucleating agents should be immiscible with the polymer matrix of the CE melt composition at the extrusion temperature of the extrusion section. As such, in some embodiments, the physical nucleating agents should have a melting temperature at least 220° C, at least 230° C of at least 240° C, at least 250° C, at least 275° C, at least 300° C, at least 325° C, or at least 350° C. Nevertheless, the physical nucleating agents may be selected such that they have the ability to, after melting, recrystallize upon cooling.

Examples of suitable inorganic physical nucleating agents include, but are not limited to, minerals such as talc, CaCOs, mica, and mixtures of at least two of the foregoing. One representative example is Heritage Plastics HT6000 Linear Low Density Polyethylene (LLDPE) Based Talc Concentrate. Other inorganic physical nucleating agents include wollastonite, silica, silicon oxide, titanium oxide, magnesium oxide, aluminum oxide and calcium silicate, barium sulfate, Kaolin, aluminum tryhydrateATH (AI(OH)3), MDH (Mg(OH)2), Diatomaceous earth, magnetite/hematite, halloysite, zinc oxide, and titanium dioxide. In some embodiments, the inorganic nucleating agents will comprise oxides, such as metal oxides or mixed metal oxides, such as those selected from one or more of the following: aluminum oxide, antimony oxide, arsenic oxide, bismuth oxide, boron oxide, calcium oxide, gallium oxide, iron oxide, lithium oxide, magnesium oxide, silicon oxide, and titanium oxide. In other embodiments, the inorganic nucleating agents will comprise silicates, such as silicates selected from one or of the following: magnesium silicate and calcium silicate. It has been discovered that biodegradable natural, particulate materials derived from renewable organic sources (e.g., organic nucleating agents) can also serve as effective physical nucleating agents. Natural materials that can be physical nucleating agents include material comprised of cellulose fibers and/or cellulose starch. Examples include, but are not limited to almond shell flour, animal fiber, apricot shell flour, bamboo flour, tree bark flour, clam shell flour, coconut shell flour, coconut coir, cork flour, corn cob flour, corn cob grit, cottonseed hulls, flock & fiber, hazelnut shell flour, kenaf flour, natural fibers, nutshell hull & flour, oat fiber powder, olive stone flour, peanut hulls flour, pecan shell flour, pine-nut shell powder, pistachio-nut shell flour, plant fiber, rice hull flour, rice hull grit, rice husk, soy bean flour, starch flour (hydrophobic), walnut shell flour, wheat chaff, wheat husk, and wood flour. Other organic physical nucleating agents include cellulose powder, chitin, chitosan, stearic acid metal salts, carbon black, and dolomite.

As noted above, suitable chemical nucleating agents (or precursors of in situ formed physical nucleating agents) are configured to decompose to create cell nucleation sites in the CE melt composition when a threshold chemical reaction temperature is reached. These small cells act as nucleation sites for larger cell growth from a physical or other type of blowing agent. In some embodiments, the precursors are configured to form a gas during extrusion of the particulate material, such as CO2 or N2.

Examples of chemical nucleating agents include but are not limited to acids, such as citric acid or a citric acid-based material. Other acids may include lauric acid, stearic acid, tartaric acid, ascorbic acid, propionic acid, and hexanoic acid. One representative example is HYDROCEROL™ CF-40E (available from Clariant Corporation), which contains citric acid and a crystal nucleating agent. In some embodiments, the chemical nucleating agents will include a combination of an acid and a base, such as a carbonate, which may include sodium bicarbonate, zinc bicarbonate, potassium bicarbonate, sodium carbonate, potassium carbonate, etc. For instance, a representative example of a chemical nucleating agent is a combination of citric acid and sodium bicarbonate. In some embodiments, chemical nucleating agents may include a carrier within which the active components of the nucleating agents are dispersed. For example, yet another representative example of chemical nucleating agents is a combination of citric acid, sodium bicarbonate, and a carrier. In some embodiments, the carrier may comprise polystyrene. However, the carrier may comprise other compositions, such as various biopolymers (e.g., polybutylene succinate, Capa polyesters, etc.), polyolefins, acrylic copolymers (e.g., ethylene methyl acrylate), or the like. In some such embodiments, the citric acid and sodium bicarbonate may comprise about half (in wt%) of the chemical nucleating agents, while the carrier makes up the remaining half (in wt%). Furthermore, in some of such embodiments, there may be more sodium bicarbonate than citric acid in the chemical nucleating agent. For instance, there may be about three times as much (in wt%) sodium bicarbonate than citric acid in the chemical nucleating agent. It should also be understood that in some embodiments, no carrier may be required or used, such as the case with the nucleating agent being Hecofoam or Hydrocerol.

In one embodiment or in combination with any of the embodiments mentioned herein, the nucleating agents are present at from 0.1 to 10 wt%, from 0.1 to 5.0 wt%, at least 0.1 wt%, at least 0.25 wt%, at least 0.5 wt% at least 1 .0 wt%, at least 1 .25 wt%, at least 1 .5 wt%, at least 1 .75 wt%, at least 2.0 wt%, at least 2.25 wt%, at least 2.5 wt%, at least 2.75 wt%, or at least 3.0 wt%, or at least 3.5 wt%, or at least 4.0 wt%, or at least 4.5 wt% and/or less than 7.5 wt%, less than 5 wt%, less than 4 wt%, less than 3 wt%, less than 2 wt%, or less than 1 .0 wt%, all based on the total weight of the cellulose ester composition. In some embodiments, the nucleating agents used herein may comprise a combination or mixture of two or more different types of nucleating agents.

It is noted that the cellulose ester material, whether in the form of compounded CE material or CE melt composition, will generally be able to accept a maximum amount of nucleating agent that can function to form nucleation sites. Any remaining nucleating agent that is added to the cellulose ester material will remain as filler. Fillers can provide various properties to the resulting cellulose ester foams and/or articles based on the type of filler used. For example, some fillers can provide increased/decreased density, ductility, Young’s modulus, yield strength, heat deflection temperature, permeability, impact resistance, elongation to break, adhesion properties, biodegradation, etc. of the cellulose ester material. Fillers can also be used to alter the visual characteristics (e.g., color, opacity, etc.) and tactile characteristics (e.g., material continuous, surface roughness, etc.) of the cellulose ester material.

Blowing Agents

A blowing agent refers to a physical or a chemical material (or combination of materials) that acts to expand nucleation sites. Blowing agents may include chemical blowing agents, physical blowing agents, combinations thereof, or several types of chemical and physical blowing agents. The blowing agents function to reduce density of a material by expanding cells formed in the molten formulation at the nucleation sites. The blowing agent may be added to the CE melt composition in the extruder. It has been surprisingly discovered that the hygroscopic nature of biodegradable particulate natural fillers allows them to absorb moisture and carry the absorbed water into the molten resin mixture where the water can act as a physical blowing agent.

Examples of physical blowing agents include H2O, N₂, CO₂, alkanes, alkenes, ethers, ketones, argon, helium, air or mixtures. In addition, it has been surprisingly discovered that the hygroscopic nature of biodegradable particulate natural fillers allows them to absorb moisture and carry the absorbed water into the molten resin mixture where the water can act as a physical blowing agent. Hygroscopic biodegradable natural fillers can be formulated into a composition and allowed to absorb moisture prior to the foaming process, where the water then is released to act as a physical blowing agent. Beneficially, the water may also be used as a plasticizer for the cellulose ester resin. Furthermore, in some embodiments, physical blowing agents may include hydrocarbons, such as pentane/isopentane or butane/isobutane. Other hydrocarbons may include propane, ethane, methane, hexane, cyclohexane, cyclopentane, cyclobutene, or the like. Chemical blowing agents are materials that degrade or react to produce a gas (e.g., CO2 or N₂). Such gasses expand the cells within the molten resin mixture and/or resulting foam mixture to produce a structural material with a plurality of gaseous voids dispersed throughout. Chemical blowing agents may be endothermic or exothermic. Chemical blowing agents typically degrade at a certain temperature to decompose and release gas. Examples of chemical blowing agents include azodicarbonamide, acids (e.g., citric acid), and carbonates, such as sodium bicarbonate, sodium carbonate, ammonium bicarbonate, ammonium carbonate, zinc carbonate, and the like and combinations thereof.

In one embodiment or in combination with any of the embodiments mentioned herein, the blowing agents described above may be combined with a secondary blowing agent (or co-blowing agent). In some embodiments, the co-blowing agent is selected from the group consisting of methyl acetate, ethanol, ketones (e.g., acetone), and mixtures thereof.

In one embodiment or in combination with any of the embodiments mentioned herein, the blowing agent (and any co-blowing agent) is present at from 0.3 to 1 .5 wt%, or 0.3 to 2.0 wt%, or 0.3 to 2.5 wt%, or 0.3 to 3.0 wt%, or 0.3 to 3.5 wt%, or 0.3 to 4.0 wt%, or 0.3 to 8%, or 1 .3 to 1 .5 wt%, or 1 .3 to 2.0 wt%, or 1 .3 to 2.5 wt%, or 1 .3 to 3.0 wt%, or 1 .3 to 3.5 wt%, or 1 .3 to 4.0 wt%, or 1 .3 to 4.5 wt%, or 1 .3 to 5.0 wt%, or 1 .3 to 5.5 wt%, or 1 .5 to 3.0 wt%, or

1 .5 to 4.0 wt%, or 1 .5 to 5.0 wt%, or 1 .5 to 6.0 wt%, or 2.0 to 3.0 wt%, or 2.0 to 4.0 wt%, or 2.0 to 5.0 wt%, or 2.0 to 6.0 wt%, or 2.5 to 3.0 wt%, or 2.5 to 4.0 wt%, or 2.5 to 5.0 wt%, or 2.5 to 6.0 wt%, or 3.0 to 4.0 wt%, or 3.0 to 5.0 wt%, or 3.0 to 6.0 wt%, or 0.0 to 9.0 wt%, or 0.5 to 9.0 wt%, or 1 .0 to 9.0 wt%, or 1 .5 to 9.0 wt%, or 2.0 to 9.0 wt%, or 2.5 to 9.0 wt%, or 3.0 to 9.0 wt%, or

3.5 to 9.0 wt%, or 4.0 to 9.0 wt%, or 4.5 to 9.0 wt%, or 5.0 to 9.0 wt%, or 5.5 to 9.0 wt%, or 6.0 to 9.0 wt%, or 6.5 to 9.0 wt%, or 7.0 to 9.0 wt%, or 7.5 to 9.0 wt%, or 8.0 to 9.0 wt%, or 8.5 to 9.0 wt%, all based on the total weight of the cellulose ester composition. In some embodiments, the blowing agents used herein may comprise a combination or mixture of two or more different types of blowing agents. Surface Modifying Additives

Surface modifying additives refer to materials that can be added to cellulose ester compositions to modify the structure of the compositions (or the resulting foam articles) to improve processing of the cellulose ester compositions. For example, the inventors of the present application have found that adding surface modifying additives to the compounded CE material (e.g., to the pellets during the compounding process) or to the CE melt composition (e.g., during the extrusion process) can improve processing by reducing unwanted sticking of the CE melt composition to the die or mandrel (or to other components of the foam sheet production process). Such reduction in sticking may be achieved by the surface modifying additives inhibiting the fusing of cellulose esters caused by plasticizers. The addition of surface modifying additives may also reduce blocking of the cellulose ester foam sheets produced at the sheet forming section. Furthermore, surface modifying additives may also improve the foam sheet production process by allowing the process to be performed at lower temperatures.

Furthermore still, in some embodiments, the surface modifying additives may function as anti-static additives, which inhibit electrical sparks or arcing in the CE melt composition. The inhibition of electrical sparks or arcing can be particularly important when hydrocarbons are used as blowing agents, so as to reduce the chance of igniting the hydrocarbons and causing fires. Beneficially, surface modifying additives may also reduce the diffusion of blowing agents, such as hydrocarbons, out of the foam sheets or resulting articles. In some embodiments, hydrocarbons themselves may be used as surface modifying additives.

Nevertheless, more general examples of surface modifying additives that may be used with compounded CE material (e.g., during the compounding process) or to the CE melt composition (e.g., during the foam sheet production process) according to embodiments of the present invention include fatty acids, such as palmitic acid, tallow acid, stearic acid, oleic acid, linoleic and linolenic acids, arachidic/behenic acids, behenic acid, and erucic acid. Surface modifying additives may also include fatty acid amides, such as erucamides, oleoamides, stearmides, bhenamides, secondary amides, and bisamides.

Additional examples of surface modifying additives may include glycerol esters and/or stearate esters, such as monoglycerides, diglycerides, and triglycerides. The monoglycerides may include glycerol monostearate or monoglyceride derivatives, such as diacetyl tartaric acid esters of mono- and diglycerides (DATEM), ethoxylated monoglyceride, succinyl monoglyceride, and propylene glycol monoesters (PGME). Examples of surface modifying additives may also include metallic stearates such as aluminum stearate, calcium stearate, lithium stearate, magnesium stearate, sodium stearate, zinc stearate, and/or combinations thereof (e.g., Calcium/Zinc stearates) . Examples of surface modifying additives may also include waxes, such as polyolefin waxes (polypropylene wax and polyethylene wax), oxidized olefin waxes, ethylene acrylic acid (EAA) copolymer waxes, ethylene methyl acrylate (EMA) copolymer waxes, EAA ionomer axes, acrylic waxes, and/or natural waxes, such as rice bran wax, sunflower wax, sugar cane wax, candelilla wax, soy wax, bees wax, candelilla wax, and carnauba waxes.

Other, non-exclusive examples of surface modifying additives include aliphatic diesters (e.g., dioctyl adipate), polyglycol diesters, alkyl alkyether diesters, aromatic triesters, polyester resins, chlorinated hydrocarbons, halogenated hydrocarbons, alkylether monoesters, and alkyl monoesters. In addition, various oils may be used as surface modifying additives, such as aromatic oils, napthenic oils, glyceride oils, silicon oils, and epoxidized oils (e.g., soybean oil and linseed oil). Thus, in some embodiments, the surface modifying additives comprise plasticizers, such as aliphatic diester plasticizers, polyester plasticizers, and the like. Furthermore, in some embodiments, surface modifying additives may comprise a polyhedral oligomeric silsesquioxane (POSS).

More generally, surface modifying additives used in embodiments of the present invention may have a lower polarity than the cellulose ester in compounded CE material (e.g., during the compounding process) or to the CE melt composition (e.g., during the foam sheet production process). For example, the surface modifying additives may have (based on Hansen solubility parameters): a total solubility parameter 5 of less than 25 MPa^1/2, less than 20 MPa^1/2, or less than 19.5 MPa^1/2; a dispersion force solubility parameter bd of less than 18 MPa^1/2, less than 16 MPa^1/2, or less than 14 MPa^1/2; a dipolar intermolecular force solubility parameter bd of less than 12 MPa^1/2, less than 8 MPa^1/2, or less than 4 MPa^1/2; and/or a hydrogen bond solubility parameter bh of less than 11 MPa^1/2, less than 10 MPa^1/2, or less than 9 MPa^1/2. However, in some other embodiments, the surface modifying additives used in embodiments of the present invention may have a higher polarity than the cellulose ester in compounded CE material (e.g., during the compounding process) or to the CE melt composition (e.g., during the foam sheet production process). For example, the surface modifying additives may have (based on Hansen solubility parameters): a total solubility parameter b of more than 21 .5 MPa^1/2, more than 23 MPa^1/2, or more than 25 MPa^1/2. In addition, in some embodiments, surface modifying additives may have a boiling point greater than 200° C, greater than 220° C, greater than 240° C, greater than 260° C, greater than 280° C, or greater than 300° C. Furthermore, the surface modifying additives may have a molecular weight greater than 100 g/mol, greater than 150 g/mol, greater than 220 g/mol, greater than 260 g/mol, greater than 300 g/mol, or greater than 340 g/mol and/or no more than 1000 g/mol, no more than 2500 g/mol, or no more than 5000 g/mol. Furthermore still, it may be preferable for the surface modifying additives to not be soluble in the plasticizer(s) used in the cellulose ester compositions. For instance, it may be preferable for the surface modifying additives to not be soluble in triacetin. Finally, in some embodiments, the surface modifying additives may be biodegradable and/or food-compliant or FDA approved.

In one embodiment or in combination with any of the embodiments mentioned herein, the surface modifying additives are present at from 0.05 to 0.75 wt%, or 0.05 to 1 .0 wt%, or 0.05 to 2.5 wt%, or 0.05 to 5.0 wt%, or 0.75 to 1 .0 wt%, or 0.75 to 2.5 wt%, or 0.75 to 5.0 wt%, or 0.1 to 1 .0 wt%, or 0.1 to 2.5 wt%, 0.1 to 5.0 wt%, or 1 .0 to 2.5 wt%, or 1 .0 to 5.0 wt%, or 2.5 to 5.0 wt%, all based on the total weight of the cellulose ester composition. In some embodiments, the surface modifying additives used herein may comprise a combination or mixture of two or more different types of surface modifying additives.

Articles

Extruded sheets of cellulose ester foam may be formed using the extrusion section and/or the sheet forming section described above. Such extruded sheets of comprise a structural material with a plurality of gaseous voids disposed throughout. Such gaseous voids are formed by expansion of the blowing agent in the form of a gas within the cellulose polymer melt. The structural material is cellulose ester based, with specific amounts of the compositional components of the structural material (e.g., cellulose ester, plasticizer, nucleating agents, surface modifying additives, etc.) having been described above in more detail. Articles may be formed from the extruded sheets of foam in accordance with embodiments, and may be particularly useful in the food service industry. Exemplary articles include meat trays. The articles may have one or more particularly advantageous properties. For example, the articles may be biodegradable and/or compostable, and/or the articles may have superior mechanical properties (e.g., strength, density, cell size, absorption, etc.).

In one embodiment or in combination with any of the embodiments mentioned herein, the foam has a density less than 0.20 g/cm³, less than 0.18 g/cm³, less than 0.15 g/cm³, less than 0.12 g/cm³, less than less than 0.10 g/cm³, less than 0.08 g/cm³, less than less than 0.06 g/cm³, or less than less than 0.04 g/cm³, or from 0.04 to 0.8 g/cm³, 0.04 to 0.6 g/cm³, 0.04 to 0.5 g/cm³, 0.04 to 0.4 g/cm³, 0.04 to 0.3 g/cm³, 0.04 to 0.2 g/cm³, 0.04 to 0.15 g/cm³, 0.04 to 0.12 g/cm³, 0.04 to 0.10 g/cm³, 0.04 to 0.08 g/cm³, 0.04 to 0.06 g/cm³, 0.06 to 0.8 g/cm³, 0.06 to 0.6 g/cm³, 0.06 to 0.5 g/cm³, 0.06 to 0.4 g/cm³, 0.06 to 0.3 g/cm³, 0.06 to 0.2 g/cm³, 0.06 to 0.15 g/cm³, 0.06 to 0.12 g/cm³, 0.06 to 0.10 g/cm³, 0.06 to 0.08 g/cm³, 0.08 to 0.8 g/cm³, 0.08 to 0.6 g/cm³, 0.08 to 0.5 g/cm³, 0.08 to 0.4 g/cm³, 0.08 to 0.3 g/cm³, 0.08 to 0.2 g/cm³, 0.08 to 0.15 g/cm³, 0.08 to 0.12 g/cm³, 0.08 to 0.10 g/cm³, 0.1 to 0.8 g/cm³, 0.1 to 0.6 g/cm³, 0.1 to 0.5 g/cm³, 0.1 to 0.4 g/cm³, 0.1 to 0.3 g/cm³, 0.1 to 0.2 g/cm³, 0.1 to 0.15 g/cm³, 0.1 to 0.12 g/cm³, 0.2 to 0.8 g/cm³, 0.2 to 0.6 g/cm³, 0.2 to 0.5 g/cm³, 0.2 to 0.4 g/cm³, 0.2 to 0.3 g/cm³, 0.3 to 0.6 g/cm³, 0.3 to 0.5 g/cm³, 0.3 to 0.4 g/cm³, 0.4 to 0.6 g/cm³, 0.4 to 0.5 g/cm³, or 0.5 to 0.6 g/cm³.

In one embodiment or in combination with any of the embodiments mentioned herein, the average foam cell size is from 40 gm to 600 gm, or 50 gm to 600 gm, or 60 gm to 600 gm, or 70 gm to 600 gm, or 80 gm to 600 gm, or 90 gm to 600 gm, or 100 gm to 600 gm, or 150 gm to 600 gm, or 200 gm to 600 gm, or 250 gm to 600 gm, or 300 gm to 600 gm, or 400 gm to 600 gm, or 500 gm to 600 gm, or 40 gm to 550 gm, or 40 gm to 500 gm, or 40 gm to 450 gm, or 40 gm to 400 gm, or 40 gm to 350 gm, or 40 gm to 300 gm, or 40 gm to 250 gm, or 40 gm to 200 gm, or 40 gm to 150 gm, or 40 gm to 100 gm.

Further Inventive Concepts Related to Processes and Systems for Producing Pellets, Foam Sheets, and/or Articles.

As described above, embodiments of the present invention include processes and systems for recovering vapors and liquids produced during the production of biodegradable compositions, sheets, and articles. These vapors and liquids may contain valuable plasticizers, physical blowing agents, and other components that would be otherwise lost or disposed of in traditional processes and systems. For example, under standard operation, the processes and methods described herein are capable of recovering, and optionally recycling, at least 0.1 gal, at least 0.5 gal, or at least 1 gal per hour (about 1 ,000 lb per hour) of plasticizer that would otherwise be lost or disposed of in traditional processes and systems.

The embodiments described herein are particularly useful in the production of cellulose ester foamed sheets and articles, although the embodiments may be utilized in other sheet and article production applications. In one embodiment or in combination with any of the embodiments mentioned herein, a biodegradable cellulose acetate foam or article may be produced that is industrial compostable or home compostable. In one subclass of this class, the foam or article is industrial compostable. In one sub-subclass of this subclass, the foam or article has a thickness that is less than 6 mm. In one sub-subclass of this subclass, the foam or article has a thickness that is less than 3 mm. In one sub-subclass of this subclass, the article has a thickness that is less than 1 .1 mm. In one subclass of this class, the foam or article is home compostable. In one sub-subclass of this subclass, the foam or article has a thickness that is less than 6 mm. In one subsubclass of this subclass, the foam or article has a thickness that is less than 3 mm. In one sub-subclass of this subclass, the foam or article has a thickness that is less than 1.1 mm. In one sub-subclass of this subclass, the foam or article has a thickness that is less than 0.8 mm. In one sub-subclass of this subclass, the foam or article has a thickness that is less than 0.6 mm. In one sub-subclass of this subclass, the foam or article has a thickness that is less than 0.4 mm.

In one embodiment or in combination with any of the embodiments mentioned herein, the thickness of the foam or article is from 1 to 10 mm, from 1 to 8 mm, from 2 to 8 mm, from 3 to 7 mm, from 4 to 6 mm, about 4 mm, about 5 mm, about 6 mm, about 7 mm, or about 8 mm. However, it should be noted that the foam or article may have other, larger sizes. For example, in some embodiments, the foam or article may have a thickness from 0.5 to 24 inches, from 1 to 15 inches, or 3 to 12 inches. Alternatively, or in addition, the tray or other article may have a thickness (i.e., the thickness of the cellulose ester foam material) from 100-400 mils, 120-300 mils, 150-250 mils.

In one embodiment or in combination with any of the embodiments mentioned herein, the foam or article exhibits greater than 90% disintegration after 12 weeks according to the disintegration test protocol for films, as described in the specification. The compositions used to prepare the biodegradable cellulose acetate foams can comprise other additives such as fillers, stabilizers, odor modifiers, waxes, compatibilizers, biodegradation promoters, dyes, pigments, colorants, lubricants, anti-oxidants, viscosity modifiers, antifungal agents, heat stabilizers, antibacterial agents, softening agents, mold release agents, UV absorbers, and combinations thereof. Each additional additive may be present in the cellulose ester-based material in an amount less than 10 wt. %, less than 5 wt. % less than 4 wt. %, less than 3 wt. %, less than 2 wt. %, or less than 1 .0 wt. %. It should be noted that the same type of compounds or materials can be identified for or included in multiple categories of components in the cellulose acetate compositions. For example, polyethylene glycol (PEG) could function as a plasticizer or as an additive that does not function as a plasticizer, such as a hydrophilic polymer or biodegradation promotor, e.g., where a lower molecular weight PEG has a plasticizing effect and a higher molecular weight PEG functions as a hydrophilic polymer but without plasticizing effect.

In one embodiment or in combination with any other embodiment mentioned herein, the foam, composition or foamable composition further comprises a photodegradation catalyst. In one class of this embodiment, the photodegradation catalyst is a titanium dioxide, or an iron oxide. In one subclass of this class, the photodegradation catalyst is a titanium dioxide. In one subclass of this class, the photodegradation catalyst is an iron oxide.

In one embodiment or in combination with any other embodiment mentioned herein, the foam, composition, or foamable composition further comprises a pigment. In one class of this embodiment, the pigment is a titanium dioxide, a carbon black, or an iron oxide. In one subclass of this class, the pigment is a titanium dioxide. In one subclass of this class, the pigment is a carbon black. In one subclass of this class, the pigment is an iron oxide. In one subclass of this class, the pigment is a biodegradable particulate natural filler. DEFINITIONS

It should be understood that the following is not intended to be an exclusive list of defined terms. Other definitions may be provided in the foregoing description, such as, for example, when accompanying the use of a defined term in context.

As used herein, the terms “a,” “an,” and “the” mean one or more.

As used herein, the terms “comprising,” “comprises,” and “comprise” are open-ended transition terms used to transition from a subject recited before the term to one or more elements recited after the term, where the element or elements listed after the transition term are not necessarily the only elements that make up the subject.

To be considered “compostable,” a material must meet the following four criteria: (1 ) the material should pass biodegradation requirement in a test under controlled composting conditions at elevated temperature (58°C) according to ISO 14855-1 (2012) which correspond to an absolute 90% biodegradation or a relative 90% to a control polymer, (2) the material tested under aerobic composting condition according to ISO16929 (2013) must reach a 90% disintegration ; (3) the test material must fulfill all the requirements on volatile solids, heavy metals and fluorine as stipulated by ASTM D6400 (2012), EN 13432 (2000) and ISO 17088 (2012); and (4) the material should not cause negative on plant growth.

As used herein, the term “biodegradable” generally refers to the biological conversion and consumption of organic molecules. Biodegradability is an intrinsic property of the material itself, and the material can exhibit different degrees of biodegradability, depending on the specific conditions to which it is exposed. The term “disintegrable” refers to the tendency of a material to physically decompose into smaller fragments when exposed to certain conditions. Disintegration depends both on the material itself, as well as the physical size and configuration of the article being tested. Ecotoxicity measures the impact of the material on plant life, and the heavy metal content of the material is determined according to the procedures laid out in the standard test method. To be considered “biodegradable,” under home composting conditions according to the French norm NF T 51-800 and the Australian standard AS 5810, a material must exhibit a biodegradation of at least 90 percent in total (e.g., as compared to the initial sample), or a biodegradation of at least 90 percent of the maximum degradation of a suitable reference material after a plateau has been reached for both the reference and test item. The maximum test duration for biodegradation under home compositing conditions is 1 year.

To be considered “biodegradable,” under industrial composting conditions according to ASTM D6400 and ISO 17088, at least 90 percent of the organic carbon in the whole item (or for each constituent present in an amount of more than 1% by dry mass) must be converted to carbon dioxide by the end of the test period when compared to the control or in absolute. According to European standard ED 13432 (2000), a material must exhibit a biodegradation of at least 90 percent in total, or a biodegradation of at least 90 percent of the maximum degradation of a suitable reference material after a plateau has been reached for both the reference and test item. The maximum test duration for biodegradability under industrial compositing conditions is 180 days.

In order to be considered “biodegradable,” under soil composting conditions according the OK biodegradable SOIL conformity mark of Vingotte and the DIN Gepruft Biodegradable in soil certification scheme of DIN CERTCO, a material must exhibit a biodegradation of at least 90 percent in total (e.g., as compared to the initial sample), or a biodegradation of at least 90 percent of the maximum degradation of a suitable reference material after a plateau has been reached for both the reference and test item. The maximum test duration for biodegradability under soil compositing conditions is 2 years. EXPERIMENTAL SECTION

Abbreviations

Min is minute(s), wt% is weight percent, Ex is example(s), g is gram(s), kg is kilogram(s), h is hour(s),

Collecting Excess Volitiles During the Extrusion Process

Cellulose acetate with processing aids can be extruded on single screw extrusion or twin screw extrusion lines. For the examples listed below, the material was extruded on a 92mm twin screw extruder and the end product was pelletized. The method; however, applies to pelletiziation, film and sheet extrusion, blow film extrusion, profile extrusion, foam extrusion and other processing needing to capture volatiles during processing.

The twin screw extruder used for this work consists of several barrel sections heated by electrical resistance and cooled by water circulating through the individual barrel sections. The extruder barrel contains two parallel screw shafts with interchangeable screw elements to perform the functions of melting, mixing, and pumping the melted material through the barrel and die. The die forms the molten material into small rods called strands which are then cooled with water and fed into a pelletizer/cutter where they are cut into pellets approximately 3.4mm x 2.8mm in size. The pellets are then sold and used in production processes including extrusion, injection molding and thermoforming into commercial products where a bio-degradable solution is desired.

The process was designed to capture volatiles generated during the extrusion process. Those volatiles any number of additives used in the process, such as a a low boiling point plasticizer, water vapor, or other volatiles from other additive types like lubricants, waxes, colorants etc. These volatiles are typically evident at the extrusion die and the extruder vacuum port/ports. Some of these volatiles will condense to a liquid upon contact with any solid surface that is lower in temperature than the process. Once condensed back into a liquid, the additive will typically be low viscosity and can cause many production problems such as clogged air conveying filters, dryer desiccant damage and safety concerns from slips and falls. Following is the method used to capture and measure the volatiles at the extruder die and the vacuum ports.

One or more of the extruder barrels will be manufactured with an open section whose purpose is to allow volatiles created during the extrusion process in the barrel to escape either into the atmosphere or to be pulled off using a vacuum pump and collected via a vacuum sweep (0 to 24 inches of mercury) and then condensed in a vacuum pot or vessel. The collected liquid is then captured for either reuse, resale or disposal. Table 1 shows that up to 40 grams per hour of liquids are collected via the vent port.

Table 1 : Collection Averages from Vacuum Pot (average of 4 to 5 measurements)

Table 2 shows that approximately 10 g/min is captured on average in the Smog Hog. The volatiles were captured at the die using a Model SHN 40 double pass electrostatic precipitator. An electrostatic precipitator consists of a pre-filter, an ionization section where an electrical charge is applied to the particles, and a collection chamber which acts as a ground capturing the positively charged particles as they exit the ionization chamber. The collected liquid is then drained off into a collection vessel. In this case a five-gallon bucket was used for convenience as each sample had to be weighted and tested for contaminates and purity. Data from an eight-day production run can be found below. Table 2. Contents draining from Dynacom SHN-40 (Smog Hog).

Collecting Excess Volitiles During the Drying Process

Cellulose acetate formulations with processing aids are susceptible to moisture uptake and must be dried before any processing takes place. The drying step will allow a volatile additive to be stripped off with water. These volatiles can then be captured via a condensation trap or demister that can be attached to the drying unit.

A Novatec NW500NC desiccant wheel dryer equipped with an internal condensation trap was used for drying the polymer. As the process air exits the hopper it blows through the filters and the coils equipped with chilled water to condense any volatiles which then drain to a holding tank to be filtered off. A total of 1800 kgs of Cellulose acetate having 18.5wt% triacetin as a plasticizers, 0.15% Doverphos 9228T and 1% epoxidized soybean oil as stabilizers was dried via 3 separate drying cycles. The condensate was collected and to evaluated for quantity and purity. Moisture results were measured by Karl Fischer titration, and the triacetin was measured using gas chromatography. The results are found in Table 3.

Table 3 : NW500NC Drying Moisture Level. Table 4 - Triacetin Loss.

Table 5. Triacetin Aid recovery.

Collecting Excess Volitiles During Final Processing

Polymer processors will take the dried pellets and process them into an extrusion process using a single screw or twin screw and/or combination of the two. This will lead to another process step where volatiles can be lost. Cellulose acetate having 18.5wt% triacetin as a plasticizers, 0.15% Doverphos 9228T and 1% epoxidized soybean oil as stabilizers was extruded on a 2.5 inch Davis Standard single screw extruder . The extruder is a 24:1 L/D having a general purpose barrier screw with a spiral maddock mixer. Conditions for this processing are recorded in Table 6.

A Smog Hog PCN with ¹/2 HP blower motor was used to cover the gap between the die and the water bath to capture the volatiles. Any other loss of the additive would have taken place in the vacuum tank water supply. The die was placed 12 inches from the sheet as seen in image 1 .

Table 6. Extruder Setpoints Table 7: Processing aid recovery after 3.8 hrs of run time.

CLAIMS NOT LIMITED TO DISCLOSED EMBODIMENTS

The preferred forms of the invention described above are to be used as illustration only and should not be used in a limiting sense to interpret the scope of the present invention. Modifications to the exemplary embodiments, set forth above, could be readily made by those skilled in the art without departing from the spirit of the present invention.

The inventors hereby state their intent to rely on the Doctrine of Equivalents to determine and assess the reasonably fair scope of the present invention as it pertains to any apparatus not materially departing from but outside the literal scope of the invention as set forth in the following claims.

Claims

CLAIMS What is claimed is:

1 . A method for recovering vapor in a cellulose ester sheet forming process, the method comprising:

(a) drying a foamable particulate composition comprising a cellulose ester and a plasticizer, thereby producing a dried particulate material;

(b) melting and extruding the dried particulate material through a die head to form an extrudate;

(c) processing the extrudate through a sheet forming system; and

(d) collecting at least a portion of a plasticizer-containing vapor produced during the drying (a), the extruding (b), and/or the processing (c).

2. A method for recovering a plasticizer in a cellulose ester sheet forming process, the method comprising:

(a) introducing a composition comprising a cellulose ester and the plasticizer to an extrusion process;

(b) melting and extruding the composition through a die head to form an extrudate;

(c) processing the extrudate through a sheet forming system;

(d) collecting at least a portion of a plasticizer-containing vapor produced during the introducing (a), the melting and extruding (b) and/or the processing (c) in a vapor collection system; and

(e) condensing at least a portion of the plasticizer-containing vapor in the vapor collection system to form a plasticizer-containing liquid.

3. The method of claim 2, wherein the vapor collection system is at least partially disposed above the extrusion process, the die head, and/or the sheet forming system.

4. The method of any one of claims 2-3, wherein the vapor collection system recovers 0.1% to 5%, 0.2 to 4%, 0.3 to 3%, 0.4 to 2%, .5% to 1% by weight of the plasticizer present in the composition.

5. A method for recovering an at least partially condensable plasticizercontaining vapor in a cellulose ester sheet forming process, the method comprising:

(a) extruding a composition through an annular die head to form a tubular extrudate;

(b) drawing the tubular extrudate over a forming mandrel;

(c) slitting the tubular extrudate with a slitting device; and

(d) recovering at least a portion of a plasticizer-containing vapor produced during the extruding (a), the drawing (b), and/or the slitting (c) in a collection system at least partially located adjacent to the die head, the mandrel, and/or the slitting device.

6. The method of claim 5, wherein the collection system is at least partially located adjacent to at least two of the die head, the mandrel, and/or the slitting device.

7. The method of any one of claims 5 or 6, further comprising collecting a condensate liquid formed on the mandrel and/or extrudate.

8. The method of any one of claims 5-7, wherein the recovering (d) comprises collecting at least a portion of the plasticizer-containing vapor in a vapor collection system at least partially disposed above the annular die head and/or the mandrel, and condensing at least a portion of the plasticizercontaining vapor in the collection system to form a plasticizer-containing liquid.

9. The method of any one of claims 5-8, wherein the vapor collection system comprises one or more vapor collection conduits and a condenser, each of the one or more conduits having an inlet at least partially positioned above the annular die and/or the mandrel.

10. The method of any one of claims 5-9, wherein the recovering (d) comprises suctioning the at least a portion of the plasticizer-containing vapor through the inlet and directing the plasticizer-containing vapor to the condenser.

11 . The method of any one of claims 5-10, wherein the inlet is positioned less than 5 feet, less than 4 feet, less than 3 feet, less than 2 feet, or less than 1 foot above the annular die and/or the mandrel.

12. The method of any one of claims 5-11 , wherein the inlet of the one or more conduits comprises a lip defining an perimeter channel, and wherein at least a portion of the plasticizer-containing vapor portion condenses in the inlet and collects as a condensate in the channel.

13. The method of any one of claims 5-12, wherein at least a portion of the condensate is drained from the channel.

14. The method of any one of claims 5-13, wherein at least a portion of the condensate drained from the channel is combined with at least a portion of the plasticizer-containing liquid.

15. The method of any one of claims 5-14, further comprising condensing at least a portion of the plasticizer-containing vapor in the vapor collection system to form a plasticizer-containing liquid.

16. The method of any one of claims 5-15, wherein the condensing (d) comprises at least partially separating the condensable components from the non-condensable components.

17. The method of any one of claim 1 -16, wherein the processing (b) comprises

(i) drawing the tubular extrudate over a forming mandrel, and

(ii) slitting the tubular extrudate.

18. The method of any one of claims 1 -17, wherein during the extruding, the drawing, and/or the slitting at least a portion of the plasticizer vaporizes to form the plasticizer-containing vapor.

19. The method of any one of claims 1 -18, wherein the plasticizer-containing vapor comprises a vaporized plasticizer component.

20. The method of any one of claims 1 -19, further comprising recycling at least a portion of the plasticizer-containing liquid into the composition before or during the extruding (a).

21 . The method of any one of claims 1-20, wherein the plasticizer-containing vapor includes one or more condensable components and one or more noncondensable components (at the processing temperatures and pressures of the extruding and/or processing steps), wherein the ratio of condensable to non-condensable components is 1 :1 to 100:1 , or 5:1 to 50:1 , or 10:1 to 20:1 .

22. The method of any one of claims 1 -21 , wherein the condensing (d) comprises at least partially separating the condensable components from the non-condensable components.

23. The method of any one of claims 1 -22, further comprising recycling at least a portion of the condensable components into the composition before or during the extruding (a), and/or recycling at least a portion of the non- condensable components into the composition during the extruding (a).

24. The method of any one of claims 1 -23, wherein the one or more noncondensable components comprises a physical blowing agent.

25. The method of any one of claims 1 -24, wherein the plasticizer-containing vapor further comprises a blowing agent (carbon dioxide (CO2)/ hydrocarbon), co-blowing agent (e.g., ketones, alcohols), vaporized water (H2O), acids (e.g., acetic acid), phosphites, oils (e.g., epoxidized soybean oil), and/or hydrocarbons (e.g., C1 -C12 hydrocarbons).

26. The method of any one of claims 1 -25, wherein the plasticizer-containing vapor comprises at least 50 percent, at least 60 percent, at least 70 percent, at least 80 percent, or at least 90 percent weight of the plasticizer, based on total weight of vapor.

27. The method of any one of claims 1 -26, wherein the plasticizer comprises glycerol triacetate (Triacetin), glycerol diacetate (Diacetin), dibutyl terephthalate, dimethyl phthalate, diethyl phthalate, polyethylene glycol) MW 200-600, dibutyl tartrate, di-2-methoxyethyl phthalate, ethyl o- benzoylbenzoate, triethylene glycol dipropionate, 1 ,2-epoxypropylphenyl ethylene glycol, 1 ,2-epoxypropyl(m-cresyl) ethylene glycol, 1 ,2-epoxypropyl(o- cresyl) ethylene glycol, p-oxyethyl cyclohexenecarboxylate, bis(cyclohexanate) diethylene glycol, triethyl citrate, polyethylene glycol, propylene glycol, polysorbate, sucrose octaacetate, acetylated triethyl citrate, acetyl tributyl citrate, Admex, tripropionin, Scandiflex, poloxamer copolymers, polyethylene glycol succinate, diisobutyl adipate, polyvinyl pyrollidone, and glycol tribenzoate, the benzoate containing plasticizers such as the Benzoflex™ plasticizer series, poly (alkyl succinates) such as poly (butyl succinate), polyethersulfones, o-Cresyl p-toluenesulfonate, n- ethyltoluenesulfonamides, adipate based plasticizers, soybean oil epoxides such as the Paraplex™ plasticizer series, sucrose based plasticizers, dibutyl sebacate, tributyrin, sucrose acetate isobutyrate, the Resolflex™ series of plasticizers, triphenyl phosphate (TPP), triethyl phosphate (TEP), glycolates (e.g., ethyl phthalyl ethyl glycolate “EPEG” and methyl phthalyl ethyl glycolate “MPEG”), methoxy polyethylene glycol, 2,2,4-trimethylpentane-1 ,3-diyl bis(2- methylpropanoate), and polycaprolactones.