SYSTEM AND METHODS FOR INJECTING COLOR DURING MANUFACTURE OF BULKED CONTINUOUS CARPET FILAMENT

Abstract

A method of introducing color to a polymer stream during the manufacturing of bulked continuous carpet filament comprises: adding a colorant to a polymer stream downstream of a primary extruder; changing a color probe within a color injection port while maintaining the flow of the polymer stream at a polymer stream pressure; using one or more static mixing assemblies for the polymer stream to substantially uniformly mix the polymer stream and its colorant; and spinning the polymer stream with its substantially uniformly mixed colorant into BCF using a spinning machine.

Description

BACKGROUND

Currently, there are many different carpet designs and colors available. Changing color probes conventionally requires shutting down the production line, which creates significant delays and associated costs.

SUMMARY

According to particular embodiments, a method of introducing liquid color to a polymer stream, and for replacing color probes, while manufacturing bulked continuous carpet filament (BCF) is provided. According to the method, a primary extruder (e.g., a multi-screw extruder such as an MRS machine) at least partially melts the polymer flakes into a polymer stream and at least partially purifies the polymer stream. The polymer stream enters a static mixing assembly having one or more individual static mixing elements (e.g., at least thirty individual static mixing elements) at an upstream end and exits at a downstream end. One or more color injection assemblies positioned prior to or along a length of the static mixing assembly provides colorant to the polymer stream. The color injection ports include a pressure blocking mechanism that activates and deactivates to fluidly couple and decouple a color probe channel of the color injection port to the polymer stream, allowing for a color probe replacement while maintaining the flow of the polymer stream at the polymer stream pressure. After mixing the polymer stream and the colorant within the static mixing assembly, the polymer stream is formed into bulked continuous carpet filament.

BRIEF DESCRIPTION OF THE DRAWINGS

Having described various embodiments in general terms, reference will now be made to the accompanying drawings, which are not necessarily drawn to scale, and wherein:

FIG. 1 depicts a high level overview of a manufacturing process for producing and coloring bulked continuous filament, according to various embodiments described herein;

FIG. 2 depicts a process flow, according to a particular embodiment, for adding a colorant and PET to a stream of molten polymer downstream from a first extruder, according to various embodiments described herein;

FIG. 3 is a perspective view of an MRS extruder that is suitable for use as the first extruder of FIG. 2, according to various embodiments described herein;

FIG. 4 is a cross-sectional view of an exemplary MRS section of the MRS extruder of FIG. 2, according to various embodiments described herein;

FIG. 5 is a cross-sectional end view of dispersion of a colorant in a stream of molten polymer prior to passing through the one or more static mixing assemblies shown in FIG. 2, according to various embodiments described herein;

FIG. 6 is a cross-sectional end view of dispersion of a colorant in a stream of molten polymer following passing through the one or more static mixing assemblies shown in FIGS. 2, according to various embodiments described herein;

FIG. 7 is a cross-sectional end view of the exemplary one of the one or more static mixing elements of FIG. 2, according to a particular embodiment, according to various embodiments described herein;

FIG. 8 is a side view of eight of the exemplary static mixing elements of FIG. 7 coupled to one another to form a static mixing assembly, according to various embodiments described herein;

FIG. 9 is a perspective view of an exemplary helical static mixing assembly, according to various embodiments described herein;

FIG. 10 is a perspective cutaway view of the helical static mixing assembly of FIG. 9 showing four helical static mixing elements, according to various embodiments described herein;

FIG. 11 depicts a process flow, according to a particular embodiment, for adding various colorants and PET to several streams of molten polymer downstream from a first extruder, according to various embodiments described herein;

FIG. 12 depicts a process flow, according to another embodiment, for adding various colorants and PET to several streams of molten polymer downstream from a first extruder, according to various embodiments described herein;

FIG. 13 depicts a side view of a static mixing assembly having individual static mixing elements coupled to one another to form a static mixing assembly and one or more color injection assemblies coupled to the static mixing assembly, according to various embodiments described herein;

FIG. 14 depicts a high level overview of a manufacturing process for producing and coloring a bulked continuous filament with a tonal color effect, according to various embodiments described herein;

FIG. 15 depicts a cross-sectional view of a polymer stream conduit with a color injection port and a polymer injection port for providing liquid colorant and PET, respectively, to a polymer stream, according to various embodiments described herein;

FIG. 16A depicts a side view of a color injection port in a closed configuration with the color probe in a retracted position, according to various embodiments described herein;

FIG. 16B depicts a side view of a color injection port in an open configuration with the color probe in a deployed position, according to various embodiments described herein;

FIG. 16C depicts a cross-sectional view of a stream engaging portion of a color injection port, illustrating leading and trailing edge flow control devices, according to various embodiments described herein;

FIGS. 17A-17B depict front, side, and top views, respectively, of a PET injection port, according to various embodiments described herein; and

FIG. 18 depicts a high level overview of a process for introducing a liquid colorant into a polymer stream during manufacturing of a bulked continuous filament, according to various embodiments described herein.

DETAILED DESCRIPTION OF VARIOUS EMBODIMENTS

Various embodiments will now be described in greater detail. It should be understood that the disclosure herein may be embodied in many different forms and should not be construed as limited to the embodiments set forth below. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the disclosure to those skilled in the art. Like numbers refer to like elements throughout.

Overview

New processes for producing and coloring fiber from recycled polymer (e.g., recycled PET polymer), virgin polymer (e.g., virgin PET polymer), and combinations of PTT and PET polymer are described below. In various embodiments, these new processes may include, for example: (1) extruding a polymer (e.g., such as PET or PTT) using a primary extruder; (2) adding a colorant to the extruded polymer downstream from the primary extruder; (3) changing a color probe within a color injection port while maintaining the flow of the extruded polymer stream at the polymer stream pressure; (4) adding other polymers (e.g., such as PET) to the extruded polymer stream if the extruded polymer stream is substantially PTT; (5) using one or more static mixing elements (e.g., up to thirty six static mixing elements or more) to substantially uniformly mix the extruded polymer and the added colorant and any added PET; and (6) using a spinning machine to spin the uniformly mixed extruded polymer and added colorant/PTT into bulked continuous filament (BCF) that has a color that is based on the added colorant. The process described herein may, for example, reduce an amount of waste related to changing a color of BCF produced using a particular extruder when switching to a different colorant.

In various embodiments, the primary extruder comprises a multi-rotating screw extruder (MRS extruder). In particular embodiments, the process further comprises: (1) splitting the molten polymer stream extruded from the primary extruder into a plurality of polymer streams (e.g., up to six polymer streams), each of the plurality of polymer streams having an associated spinning machine; (2) adding a colorant to each split polymer stream; (3) adding other polymers (e.g., such as PET) to the extruded polymer stream if the extruded polymer stream is substantially PTT; (4) using one or more static mixing assemblies for each split polymer stream to substantially uniformly mix each split polymer stream and its respective colorant and other additives; and (5) spinning each polymer stream with its substantially uniformly mixed colorant and any additives into BCF using the respective spinning machine. In such embodiments, a process for producing and coloring bulked continuous filament may utilize a single primary extruder to produce a plurality of different colored filaments (e.g., carpet yarn).

In various embodiments, this new process may, for example: (1) produce less waste than other processes when producing or changing a color of BCF produced using a particular extruder, saving time, money, and product; (2) facilitate the production of small batches of particular colors of filament (e.g., for use in rugs or less popular colors of carpet) at a relatively low cost; (3) increase a number of simultaneous filament colors that a single extruder can produce; (4) allow for flexibility in manufacturing equipment and production line configurations while maintaining a satisfactory mix time for a PET and PTT mixture prior to spinning; and (5) otherwise streamline the manufacture of PET and PTT carpet filament, while providing for multiple colorant capabilities.

The various embodiments below will be described in both the context of utilizing virgin or recycled PET polymer to create BCF and in the context of utilizing PTT to create BCF. When virgin or recycled PET is used to create BCF, additional polymers are not described as being added, just colorant. However, when making BCF using PTT, other polymers are added to improve flammability and other characteristics of the resulting BCF. The embodiments herein will be described in the context of adding PET to a PTT stream. When PET or other polymers are added to a stream of PTT and the mixture undergoes extrusion and mixing for an extended time period, a chemical process called transesterification may occur. Transesterification results in a mixture that is difficult to spin in the spinning machines.

Traditionally, transesterification is a factor because the time between adding PET to the PTT stream and spinning the resulting polymer stream into BCF (this time period will be referred to herein as the “hold up time”) is such that the transesterification may occur. However, when utilizing production lines that employ a primary extruder on a primary line before splitting the primary line into a number of secondary lines, each with secondary extruders and static mixing assemblies, as described in the various embodiments below, transesterification may impede the spinning process. Accordingly, rather than adding PET or other polymers to the PTT stream at the primary extruder, as is traditionally done, embodiments described below provide for the addition of PET or other polymers to the PTT stream downstream of the primary extruder. The PET addition may occur at the secondary extruders, at the static mixing assemblies, or within the static mixing assemblies (e.g., or in one or more dynamic mixing assemblies). Doing so significantly shortens the hold up time, which improves the characteristics of the mixed polymer stream prior to spinning the polymer mixture into BCF.

According to other aspects of the disclosure below, systems and methods provide for improved colorant additions to polymer streams and color injection ports that allow for the removal and replacement of color probes without requiring a shut down of the production line. Embodiments herein provide for liquid colorant injections into a centered position of the polymer stream while maintaining laminar flow characteristics of the polymer stream. Color injection ports accurately place the color probe within the polymer stream while providing for retraction and insertion of the color probe while maintaining the polymer stream at the desired polymer stream pressure. The color injection ports prevent a backflow of the polymer stream through the color injection port when the color probe is removed and replaced. In this manner, the production line may continue to run during color probe replacement, saving the significant amount of time and corresponding costs associated with stopping and starting the production line that is required in conventional color probe replacements.

More Detailed Discussion

FIG. 1 depicts a high level overview of BCF manufacturing process 100 for producing and coloring BCF, for example, for use in the production of carpet and other products. The BCF manufacturing process, according to various embodiments, may generally be broken down into five operations: (1) passing polymer flakes (e.g., PET or PTT) through an extruder that melts the flakes and purifies the resulting polymer (Operation 102) to create a polymer stream; (2) optionally splitting the extruded polymer stream into a plurality of polymer streams and adding a colorant to each of the plurality of polymer streams (Operation 104); (3) adding PET downstream of the primary extruder if the polymer stream is PTT (Operation 106) (if the polymer stream is PET, according to one embodiment, no further PET or other polymers are added); (4) using one or more static mixing assemblies to substantially uniformly mix each of the plurality of polymer streams with its respective added colorant and PET, if applicable (Operation 108); and (5) feeding each of the substantially uniformly mixed and colored plurality of polymer streams into a respective spinning machine that turns the polymer into filament for use in manufacturing carpets (Operation 110). These five operations are described in greater detail below.

Operation 1: Using an Extrusion System to Melt and Purify PET or PTT

In various embodiments, the operation of using an extrusion system to melt and purify PET (e.g., PET flakes and/or pellets) or PTT comprises: (A) preparing the PET or PTT for extrusion; and (B) using a suitable extruder to melt and purify the PET or PTT. As discussed above, the embodiments herein apply to both the processing of PET into BCF, as well as the processing of PTT into BCF. It should be understood that the description with respect to the preparation and processing of PET and with respect to the preparation and processing of PTT are interchangeable, with minor exceptions. In other words, if a process is described with respect to processing a PET stream into a colored BCF product, it should be appreciated that the same process applies to a PTT stream, with a couple of exceptions.

The exceptions include the processing of recycled PET preparation and the addition of PET to a PTT stream. The discussion of preparing recycled consumer materials into PET flakes to create the PET stream does not apply to PTT since PTT does not originate from recycled consumer materials. Moreover, when discussing the processing of a PTT stream into a colored BCF product, PET is added in the manner described below in order to improve the flammability and other characteristics of the resulting product. The PET addition is not applicable to the processing of a PET stream as there would be little benefit to doing so.

A. Preparing the PET or PTT for Extrusion

In particular embodiments, the operation of preparing the PET for extrusion may vary based on a source of the PET. For example, in various embodiments, the process may utilize: (1) virgin PET (e.g., virgin PET pellets); (2) recycled PET (e.g., recycled PET flakes ground from recycled PET bottles and other suitable sources); and/or (3) a combination of virgin and recycled PET. In various embodiments in which the process utilizes recycled PET, the operation of preparing the PET for extrusion may include sorting, grinding, washing and other operations designed to remove any (e.g., some) impurities from the recycled PET prior to extrusion. These other PET preparation operations may, for example, be unnecessary in embodiments of the process that utilize virgin PET or that utilize PTT. Because using recycled PET in the process described herein may contribute to even further costs savings to those associated with a reduction in waste due to colorant changing, the process will be described below particularly with respect to recycled PET.

In a particular embodiment, preparing the PET for extrusion may include preparing flakes of PET polymer from post-consumer bottles or other sources of recycled PET. An exemplary process for preparing post-consumer bottles for use in the production of bulked continuous filament is described in U.S. Pat. No. 8,597,553 B1, entitled “Systems and Methods for Manufacturing Bulked Continuous Filament” and published on Dec. 3, 2013, which is hereby incorporated herein in its entirety. Generally speaking, the operation of preparing flakes of PET polymer from post-consumer bottles may comprise, for example: (A) sorting post-consumer PET bottles and grinding the bottles into flakes; (B) washing the flakes; and (C) identifying and removing any impurities or impure flakes.

Sorting Post-Consumer PET bottles and Grinding the Bottles into Flakes

In particular embodiments, bales of clear and mixed colored recycled post-consumer (e.g., “curbside”) PET bottles (or other containers) obtained from various recycling facilities make-up the post-consumer PET containers for use in the process. In other embodiments, the source of the post-consumer PET containers may be returned ‘deposit’ bottles (e.g., PET bottles whose price includes a deposit that is returned to a customer when the customer returns the bottle after consuming the bottle's contents). The curbside or returned “post-consumer” or “recycled” containers may contain a small level of non-PET contaminates. The contaminants in the containers may include, for example, non-PET polymeric contaminants (e.g., PVC, PLA, PP, PE, PS, PA, etc.), metal (e.g., ferrous and non-ferrous metal), paper, cardboard, sand, glass or other unwanted materials that may find their way into the collection of recycled PET. The non-PET contaminants may be removed from the desired PET components, for example, through one or more of the various processes described below.

In particular embodiments, smaller components and debris (e.g., components and debris greater than 2 inches in size) are removed from the whole bottles via a rotating trammel. Various metal removal magnets and eddy current systems may be incorporated into the process to remove any metal contaminants. Near Infra-Red optical sorting equipment such as the NRT Multi Sort IR machine from Bulk Handling Systems Company of Eugene, Oreg., or the Spyder IR machine from National Recovery Technologies of Nashville, Tenn., may be utilized to remove any loose polymeric contaminants that may be mixed in with the PET flakes (e.g., PVC, PLA, PP, PE, PS, and PA). Additionally, automated X-ray sorting equipment such as a VINYLCYCLE machine from National Recovery Technologies of Nashville, Tenn. may be utilized to remove remaining PVC contaminants.

In particular embodiments, the sorted material is taken through a granulation operation (e.g., using a 50B Granulator machine from Cumberland Engineering Corporation of New Berlin, Wisconsin) to size reduce (e.g., grind) the bottles down to a size of less than one half of an inch. In various embodiments, the bottle labels are removed from the resultant “dirty flake” (e.g., the PET flakes formed during the granulation operation) via an air separation system prior to entering the wash process.

Washing the Flakes

In particular embodiments, the “dirty flake” is then mixed into a series of wash tanks. As part of the wash process, in various embodiments, an aqueous density separation is utilized to separate the olefin bottle caps (which may, for example, be present in the “dirty flake” as remnants from recycled PET bottles) from the higher specific gravity PET flakes. In particular embodiments, the flakes are washed in a heated caustic bath to about 190 degrees Fahrenheit. In particular embodiments, the caustic bath is maintained at a concentration of between about 0.6% and about 1.2% sodium hydroxide. In various embodiments, soap surfactants as well as defoaming agents are added to the caustic bath, for example, to further increase the separation and cleaning of the flakes. A double rinse system then washes the caustic from the flakes.

In various embodiments, the flake is centrifugally dewatered and then dried with hot air to at least substantially remove any surface moisture. The resultant “clean flake” is then processed through an electrostatic separation system (e.g., an electrostatic separator from Carpco, Inc. of Jacksonville, Fla.) and a flake metal detection system (e.g., an MSS Metal Sorting System) to further remove any metal contaminants that remain in the flake. In particular embodiments, an air separation operation removes any remaining label from the clean flake. In various embodiments, an electro-optical flake sorter based at least in part on Raman technology (e.g., a Powersort 200 from Unisensor Sensorsysteme GmbH of Karlsruhe, Germany) performs the final polymer separation to remove any non-PET polymers remaining in the flake. This operation may also further remove any remaining metal contaminants and color contaminants.

In various embodiments, the combination of these steps delivers substantially clean (e.g., clean) PET bottle flake comprising less than about 50 parts per million PVC (e.g., 25 ppm PVC) and less than about 15 parts per million metals for use in the downstream extrusion process described below.

Identifying and Removing Impurities and Impure Flakes

In particular embodiments, after the flakes are washed, they are fed down a conveyor and scanned with a high-speed laser system 300. In various embodiments, particular lasers that make up the high-speed laser system 300 are configured to detect the presence of particular contaminates (e.g., PVC or Aluminum). Flakes that are identified as not consisting essentially of PET may be blown from the main stream of flakes with air jets. In various embodiments, the resulting level of non-PET flakes is less than 25 ppm.

In various embodiments, the system is adapted to ensure that the PET polymer being processed into filament is substantially free of water (e.g., entirely free of water). In a particular embodiment, the flakes are placed into a pre-conditioner for between about 20 and about 40 minutes (e.g., about 30 minutes) during which the pre-conditioner blows the surface water off of the flakes. In particular embodiments, interstitial water remains within the flakes. In various embodiments, these “wet” flakes (e.g., flakes comprising interstitial water) may then be fed into an extruder (e.g., as described below), which includes a vacuum setup designed to remove—among other things—the interstitial water that remains present in the flakes following the quick-drying process described above.

B. Using an Extrusion System to Melt and Purify PET or PTT Flakes

FIG. 2 depicts an exemplary process flow for producing BCF with an added colorant according to particular embodiments. As shown in FIG. 2, in various embodiments, a suitable primary extruder 202 is used to melt and purify PTT 200, such as any suitable PTT 200 prepared in any manner described above. In a particular embodiment, the primary extruder 202 comprises any suitable extruder such as, for example, a Multiple Rotating Screw (“MRS”) extruder, a twin screw extruder, a multiple screw extruder, a planetary extruder, or any other suitable extrusion system. An exemplary MRS Extruder 400 is shown in FIGS. 3 and 4. A particular example of such an MRS extruder is described in U.S. Published Patent Application 2005/0047267, entitled “Extruder for Producing Molten Plastic Materials”, which was published on Mar. 3, 2005, and which is hereby incorporated herein by reference.

As may be understood from FIGS. 3 and 4, in particular embodiments, the MRS extruder includes a first single-screw extruder section 410 for feeding material into an MRS section 420 and a second single-screw extruder section 440 for transporting material away from the MRS section.

As may be understood from FIG. 3, in various embodiments, PET is first fed through the MRS extruder's first single-screw extruder section 410, which may, for example, generate sufficient heat (e.g., via shearing) to at least substantially melt (e.g., melt) the wet flakes.

The resultant polymer stream (e.g., comprising the melted PET), in various embodiments, is then fed into the extruder's MRS section 420, in which the extruder separates the polymer flow into a plurality of different polymer streams (e.g., 4, 5, 6, 7, 8, or more streams) through a plurality of open chambers. FIG. 4 shows a detailed cutaway view of an MRS Section 420 according to a particular embodiment. In particular embodiments, such as the embodiment shown in this figure, the MRS Section 420 separates the polymer flow into eight different streams, which are subsequently fed through eight satellite screws 425A-H. As may be understood from FIG. 3, in particular embodiments, these satellite screws are substantially parallel (e.g., parallel) to one other and to a primary screw axis of the MRS Machine 400.

As shown in FIG. 4, in particular embodiments: (1) the satellite screws 425A-H are arranged within a single screw drum 428 that is mounted to rotate about its central axis; and (2) the satellite screws 425A-H are configured to rotate in a direction that is opposite to the direction in which the single screw drum rotates 428. In various other embodiments, the satellite screws 425A-H and the single screw drum 428 rotate in the same direction. In particular embodiments, the rotation of the satellite screws 425A-H is driven by a ring gear. Also, in various embodiments, the single screw drum 428 rotates about four times faster than each individual satellite screw 425A-H. In certain embodiments, the satellite screws 425A-H rotate at substantially similar (e.g., the same) speeds.

In various embodiments, as may be understood from FIG. 4, the satellite screws 425A-H are housed within respective extruder barrels, which may, for example be about 30% open to the outer chamber of the MRS section 420. In particular embodiments, the rotation of the satellite screws 425A-H and single screw drum 428 increases the surface exchange of the polymer stream (e.g., exposes more surface area of the melted polymer to the open chamber than in previous systems). In various embodiments, the MRS section 420 creates a melt surface area that is, for example, between about twenty and about thirty times greater than the melt surface area created by a co-rotating twin screw extruder. In a particular embodiment, the MRS section 420 creates a melt surface area that is, for example, about twenty-five times greater than the melt surface area created by a co-rotating twin screw extruder.

In various embodiments, the MRS extruder's MRS Section 420 is fitted with a vacuum pump that is attached to a vacuum attachment portion 422 of the MRS section 420 so that the vacuum pump is in communication with the interior of the MRS section via a suitable opening 424 in the MRS section's housing. In still other embodiments, the MRS Section 420 is fitted with a series of vacuum pumps. In particular embodiments, the vacuum pump is configured to reduce the pressure within the interior of the MRS Section 420 to a pressure that is between about 0.5 millibars and about 25 millibars. In particular embodiments, the vacuum pump is configured to reduce the pressure in the MRS Section 420 to less than about 5 millibars (e.g., about 1.8 millibars or less). The low-pressure vacuum created by the vacuum pump in the MRS Section 420 may remove, for example: (1) volatile organics present in the melted polymer as the melted polymer passes through the MRS Section 420; and/or (2) at least a portion of any interstitial water that was present in the wet flakes when the wet flakes entered the MRS Extruder 400. In various embodiments, the low-pressure vacuum removes substantially all (e.g., all) of the water and contaminants from the polymer stream.

In some embodiments, after the molten polymer is run the through the multi-stream MRS Section 420, the streams of molten polymer are recombined and flow into the MRS extruder's second single screw section 440. In particular embodiments, passage through the low pressure MRS Section 420 purifies the recycled polymer stream (e.g., by removing the contaminants and interstitial water) and makes the recycled polymer substantially structurally similar to (e.g., structurally the same as) pure virgin PET polymer. In particular embodiments, the resulting polymer is a recycled PET polymer (e.g., obtained 100% from post-consumer PET products, such as PET bottles or containers) having a polymer quality that is suitable for use in producing PET carpet filament using substantially only (e.g., only) PET from recycled PET products.

Operation 2: Add a Colorant to the Polymer Stream Downstream from the Primary Extruder

In particular embodiments, after the recycled PET polymer, virgin PET, or PTT has been extruded and purified by the above-described extrusion process, a colorant is added to the resultant polymer stream. FIG. 2 shows a polymer stream of PTT 200 passing through a primary extruder 202 before Colorant A 204 and PET 220 are added via a secondary extruder 206. FIG. 2 is equally applicable to implementations in which the polymer stream being processed is PET 220.

The secondary extruder 206 may include any suitable extruder such as for example, any suitable single-screw extruder or other extruder described herein (e.g., a twin screw extruder, a multiple screw extruder, a planetary extruder, or any other suitable extrusion system). In particular embodiments, a suitable secondary extruder 206 may include, for example, an HPE-150 Horizontal Extruder manufactured by David-Standard, LLC of Pawcatuck, Conn.

Colorant A 204 may comprise pelletized color concentrate which the secondary extruder 206 is configured to at least partially melt prior to adding Colorant A 204 to the polymer stream. In various other embodiments, Colorant A 204 may comprise other additives such as, for example, a carrier resin which may aid in binding the colorant to the polymer. In other embodiments, Colorant A 204 may include any suitable liquid colorant which may be pumped into the polymer stream using any suitable pump (e.g., in lieu of using a secondary extruder 206 and pelletized color concentrate).

In various embodiments, the process may further include monitoring an amount of throughput (e.g., polymer output) from the primary extruder 202 in order to determine an appropriate amount of letdown (e.g., an appropriate letdown ratio) such that a proper amount of Colorant A 204 is added to the polymer stream downstream from the primary extruder 202. In various embodiments, a desirable letdown ratio may include a letdown ratio of between about one tenth of one percent and about eight percent (e.g., about two percent). In other embodiments, the letdown ratio may include any other suitable letdown ratio (e.g., one percent, two percent, three percent, four percent, five percent, six percent, seven percent, etc.). In particular embodiments, the letdown ratio may vary based on a desired color of BCF ultimately produced using the process (e.g., up to about twenty percent).

In various embodiments, adding the colorant 204 downstream of the primary extruder 202 may save on waste during color changeover. For example, when switching between producing BCF of a first color to producing BCF of a second color, it is necessary to change the colorant 204 added to the polymer stream (e.g., from a first colorant that would result in BCF of the first color to a second colorant that would result in BCF of the second color). As may be understood by one skilled in the art, after switching from adding the first colorant to the polymer stream to adding the second colorant to the polymer stream, residual first colorant may remain in in the system between the point in the process at which the colorant is added and the spinning machine 212. For example, residual first colorant may remain in the secondary extruder 206, the one or more static mixing assemblies 208, or any other physical mechanism used in the process (such as any mechanism shown in FIG. 2) or any piping or tubing which connects the various components of the system.

As may be understood by one skilled in the art, after running the process with the second colorant for a suitable amount of time, the BCF produced by the process will eventually be of the second, desired color (e.g., because the first colorant will eventually be substantially flushed out the system). Between the point at which there is a changeover in adding the second colorant to the process rather than the first colorant and the point at which the process begins to produce the desired color of BCF, the process will produce some waste BCF that is of an undesired color (e.g., due at least in part to the residual first colorant).

In various embodiments, the waste BCF produced using the process described herein may be considerably lower than waste BCF produced during color changeovers using other processes (e.g., such as other processes in which colorant is added to PET prior to extrusion in a primary extruder such as an MRS extruder). For example, in various embodiment, the process described herein may limit waste BCF to an amount of BCF produced when running a single package of colorant (e.g., of the second colorant), which may, for example, result in less than about 100 pounds of waste. In particular embodiments, reducing waste may lead to cost saving in the production of BCF.

Operation 3: Adding PET to the Extruded Polymer Stream if the Extruded Polymer Stream is Substantially PTT

According to one embodiment shown in FIG. 2, the polymer stream being processed is a PTT 200 polymer stream. In this example, rather than adding the desired quantity of PET 220 to the primary extruder 202, as conventionally done, the PET 220 may be added to the secondary extruder 206 with the Colorant A 204. This overall configuration might be advantageous if there is other equipment or production line configuration issues that extend the length of the production line to a degree that would create excessive hold up times resulting in undesirable transesterification if the PET 220 were added at the primary extruder 202 rather than downstream at the secondary extruder 206, as shown. The addition of PET into a stream of PTT will be discussed in further detail with respect to embodiments shown in FIGS. 11 and 12. Structural aspects of a polymer injection port for providing PET 220 into the polymer stream of PTT 200 will be described with respect to FIGS. 15 and 17A-17C.

Operation 4: Use One or More Static Mixing Assemblies to Mix Polymer Stream with Added Colorant

In particular embodiments, following the addition of Colorant A 204 to the stream of molten polymer, the process includes the use of one or more static mixing assemblies 208 (e.g., one or more static mixing elements) to mix and disperse Colorant A 204 throughout the polymer stream. As may be understood by one skilled in the art, due in part to the viscosity of the polymer stream (e.g., polymer stream), when a dye or other colorant is added to the polymer stream, the dye and the stream may not mix. In various embodiments, the flow of the polymer stream is substantially laminar (e.g., laminar) which may, for example, further lead to a lack of mixing. FIG. 5 depicts a cross section view of a polymer stream conduit 500 containing a polymer stream 510 into which a colorant 520 has been added. As shown in this Figure, the colorant 520 has not mixed with the polymer stream 510. Generally speaking, the unmixed polymer stream 510 and colorant 520 may not be suitable for forming into BCF (e.g., because the resulting filament may not have a consistent, uniform color). FIG. 6 depicts the polymer stream conduit 500 of FIG. 5 in which the colorant 520 and the polymer stream 510 have been substantially thoroughly (e.g., uniformly) mixed into a colored polymer stream 530. This substantially uniform mixing, in various embodiments, is achieved through the use of the one or more static mixing assemblies 208 as shown in FIG. 2. Generally speaking, this uniformly mixed colored polymer stream 530 shown in FIG. 5 may be far more suitable for producing uniformly colored BCF.

FIG. 7 depicts an exemplary static mixing element 700 which may, in various embodiments, be utilized in the achievement of substantially uniform (e.g., uniform) mixing of the polymer stream and the added colorant (e.g., Colorant A 204 from FIG. 2). As may be understood from this Figure, a static mixing element 700 may comprise a housing 702 (e.g., a substantially circular or cylindrical housing) and be inserted into a polymer stream conduit or other housing (e.g., incorporated into a polymer stream conduit or other housing). In the embodiment shown in this Figure, the static mixing element 700 comprises a plurality of mixing bars 704 disposed within the housing 702. In particular embodiments, the static mixing element 700 creates mixing by directing two or more viscous materials to follow the geometric structure of the mixing bars 704 disposed within the housing 702 that continuously divide and recombine the flow. In various embodiments, a very high degree of mixing may be achieved over a short length of static mixing elements. In particular embodiments, the static mixing element 700 comprises no moving parts and is made of any suitable material such as, for example high strength heat treated stainless steel, a suitable plastic, or any other suitable material.

In particular embodiments, the static mixing assemblies 208 shown in FIG. 2 comprise any suitable static mixing element, such as, for example, a Stamixco GXR 40/50 or GXR 52/60 made by Stamixco LLC of Brooklyn, N.Y. A suitable mixing element for use as or within a static mixing assembly is described in U.S. Pat. No. 8,360,630 B2, entitled “Mixing Elements for a Static Mixer and Process for Producing Such a Mixing Element” and published on Jan. 29, 2013, which is hereby incorporated herein in its entirety. In other embodiments, the one or more static mixing assemblies 208 may comprise any other suitable static mixing element having a suitable arrangement of mixing bars for dispersing the colorant throughout the polymer stream. In particular embodiments, the one or more static mixing assemblies 208 comprise a plurality of individual static mixing elements 700 such as is shown in FIG. 8. FIG. 8 depicts eight static mixing elements 700a-h coupled to one another to form a static mixing assembly 208. In other embodiments, the static mixing assemblies 208 may comprise any suitable number of individual static mixing elements 700 (e.g., up to 36 or 40 individual static mixing elements). In particular embodiments, the individual static mixing elements 700 may be oriented in any suitable direction relative to one another (e.g., oriented randomly relative to one another when coupled to one another as shown in FIG. 8). In other embodiments, the static mixing elements may be oriented such that they alternate a horizontal and vertical alignment relative to one another. In still other embodiments, each adjacent static mixing element is substantially perpendicular to the adjacent static mixing element. In still other embodiments, the individual static mixing elements may be arranged in any suitable unaligned manner.

In various other embodiments, the static mixing assemblies 208 may comprise a suitable number of static mixing elements comprising one or more suitable helical mixing elements. FIG. 9 depicts an exemplary helical static mixing assembly 900 comprising a substantially cylindrical (e.g., cylindrical) housing 902 in which at least one helical mixing element 904 is disposed). As shown in this Figure, the at least one helical mixing element 904 defines a leading edge 906 that extends between opposing interior portions of the cylindrical housing (e.g., along a diameter of the cylindrical housing). In various embodiments, the leading edge 906 is substantially planar (e.g., linear) and has any suitable thickness. As may be understood from this Figure, the leading edge 906 may divide (e.g., bisect) a polymer stream flowing into the helical static mixing assembly 900 into two streams (e.g., a first stream on a first side of the leading edge 906 and a second stream on a second side). In particular embodiments, the leading edge may divide the flow into substantially equal streams as material passes the helical mixing element 904.

FIG. 10 depicts the helical static mixing assembly 900 of FIG. 9 in a cutaway view that shows four helical mixing elements 904 disposed within the housing 902. As may be further understood from FIG. 10, each individual helical mixing element 904 (e.g., helical mixing element 904a) comprises a substantially rectangular (e.g., rectangular) plate defining a leading edge 906a and a trailing edge 908a that has been twisted about 180 degrees (e.g., 180 degrees). As shown in this Figure, the leading edge 906a and trailing edge 908a are substantially parallel (e.g., parallel) to one another and the helical mixing element 904a extends between the leading edge 906a and trailing edge 908a in a helical pattern. Although in the embodiment shown in this Figure, the helical mixing element 904a is shown having a twist of 180 degrees between the leading edge 906a and trailing edge 908a, it should be understood that in various other embodiments, each individual helical mixing element 904 may comprise any other suitable helical shape or portion thereof. For example, in particular embodiments, the helical mixing element 904 may comprise a substantially rectangular plate defining a leading edge 906 and a trailing edge 908 that has been twisted any other suitable amount between zero and 360 degrees (e.g., 45 degrees, 90 degrees, 270 degrees, etc.) In still other embodiments, the helical mixing element 904 may have any suitable length relative to its diameter.

As may be further understood from FIG. 10, in various embodiments, each particular helical mixing element 904a-d is disposed within the housing 902 at an angle to an adjacent helical mixing element 904. For example, helical mixing element 904a is disposed such that a trailing edge 908a of helical mixing element 904a forms an angle with the leading edge 906b of helical mixing element 906b. In particular embodiments, the trailing edge 908a and leading edge 906b of adjacent helical mixing elements 904 may form any suitable angle with one another. In particular embodiments, the trailing edge 908a and leading edge 906b of adjacent helical mixing elements 904 may form an angle of between about zero degrees and about ninety degrees with one another. In particular embodiments, the trailing edge 908a and leading edge 906b of adjacent helical mixing elements 904 may at least partially abut one another and be substantially co-facing (e.g., co-facing). In particular embodiments, the trailing edge 908a and leading edge 906b of adjacent helical mixing elements 904 may form a particular angle between one another (e.g., zero degrees, ninety degrees, forty-five degrees, or any other suitable angle). A suitable helical static mixing assembly for use in the above-described process may include, for example, the any suitable helical static mixing assembly manufactured by JLS International of Charlotte, N.C.

It should be understood that for the purposes of this disclosure, a static mixing assembly 208 may be configured in any desired arrangement to provide a desired number of one or more individual mixing elements to a polymer stream. For example, a static mixing assembly 208 may include a single mixing element within a single housing with one or more mixing bars 704 and/or one or more helical mixing elements 904 disposed within the housing. Alternatively, the static mixing assembly 208 may include multiple static mixing elements positioned in series within a single housing. According to yet another alternative embodiment, the static mixing assembly 208 may include a plurality of static mixing elements, each having their own respective housing positioned in series adjacent to one another. In this embodiment, the plurality of static mixing elements are collectively considered the static mixing assembly 208. For example, in particular embodiments, the static mixing assembly 208 comprises up to thirty-six individual static mixing elements (e.g., thirty-six static mixing elements, thirty-four static mixing elements, etc.). In still other embodiments, the static mixing assembly 208 comprises any other suitable number of static mixing elements sufficient to substantially uniformly (e.g., homogeneously) mix the molten polymer with the added colorant (e.g., to substantially uniformly mix the molten polymer and the added colorant into a colored polymer stream 530 as shown in FIG. 6). This may include, for example, up to 40 static mixing elements, or any other suitable number).

In particular embodiments, the one or more static mixing assemblies 208 may comprise any suitable combination of static mixing elements such as, for example, any suitable break down of the static mixing element 700 shown in FIG. 7 and the helical static mixing assembly 900 and/or helical mixing elements 904 shown in FIGS. 9 and 10. For example, in a particular embodiment, the static mixing assemblies 208 may comprise thirty-six helical mixing elements 904. In other embodiments, the static mixing assemblies 208 may comprise thirty-six static mixing elements 700 from FIG. 7. In various embodiments, the static mixing assemblies 208 may comprise any suitable number of alternating static mixing elements 700 shown in FIG. 7 and helical mixing elements 904 shown in FIGS. 9 and 10. In various other embodiments, the static mixing assemblies 208 may comprise up to a total of forty (e.g., thirty-six), or more, individual static mixing elements 700 shown in FIG. 7 and helical mixing elements 904 shown in FIGS. 9 and 10. In such embodiments, the static mixing elements 700 from FIG. 7 and the helical mixing elements 904 may be arranged in any suitable order (e.g., a specific order, a random order, a pattern such as a repeating pattern, etc.).

Creating a Tonal Color in Polymer Stream

According to various embodiments, it may be desirable to create BCF for use in the production of carpet and other products that is not uniform in color. Specifically, it may be desirable to create BCF that has a tonal color effect. For the purposes of this disclosure, BCF having a tonal color effect may include BCF having any color that is not uniform, such as BCF that includes different shades of the same color (e.g., with gradual changes between one shade to another). Conventionally, tonal color effects may be created using one or more yarns or filaments having one dark end and one light end, which are twisted together to create a tonal yarn. However, using the concepts and technologies described herein, a tonal color effect may be created using a single yarn, without utilizing the conventional twisting process.

According to one embodiment, the tonal effect characteristic of the polymer stream and resulting BCF product may be created using a smaller number of static mixing elements (individual static mixing elements 700 or helical mixing elements 904) as compared to the at least thirty individual static mixing elements utilized to create the uniformly mixed and uniformly colored polymer streams described above. For example, according to one implementation, a smaller number of individual static mixing elements 700 or helical static mixing elements 904 (e.g., any discrete number less than thirty) may be used to create the static mixing assemblies 208 of FIG. 2. By using a relatively small number of individual static mixing elements, in various embodiments, the colorant injected into the laminar flow of the polymer stream traversing through the static mixing assemblies 208 is not uniformly mixed into the polymer stream prior to being received by the spinning machine 212.

While, in various embodiments, providing a static mixing assembly 208 with fewer individual static mixing elements (i.e., static mixing elements 700 or helical static mixing elements 904) may create a tonal color characteristic in the resulting polymer stream, various embodiments described herein may produce tonal color effects, while allowing for the same BCF manufacturing system to be utilized to create both uniformly-colored BCF and BCF having tonal color effects with, in various embodiments, minimal time and effort in changing the system set up between manufacturing runs of the two products.

Turning to FIG. 13, a static mixing assembly 208 is shown having a number of individual static mixing elements 700, 904 coupled together to create a length of the static mixing assembly 208 through which the polymer stream flows and mixes. It should be appreciated that for clarity purposes, the static mixing assembly 208 is shown with a reduced quantity of individual static mixing elements 700, 904 shown in FIG. 13. As disclosed herein, the static mixing assembly 208 of various embodiments may have more than thirty (i.e., thirty six or forty) individual static mixing elements 700, 904.

According to various embodiments, the static mixing assembly 208 has one or more color injection assemblies 1302a-n (collectively referred to as color injection ports 1302), and/or liquid injection nozzles, positioned along a length of the static mixing assembly 208. The one or more color injection assemblies 1302 may include any type of port suitable for facilitating the injection of colorant from one or more color probes 1304 into the polymer stream within the static mixing assembly 208. According to one embodiment, the one or more color injection assemblies 1302 include threads for receiving the one or more color probes 1304 and/or one or more mechanisms coupled to the one or more color probes 1304. In other embodiments, the one or more color injection assemblies 1302 and the one or more color probes 1304 are coupled together via a quick disconnect connection 1306 that allows for easy and rapid connection of the one or more color probes 1304 to/from the color injection ports 1302. Various features of color injection ports 1302 according to various embodiments will be described in detail below with respect to FIGS. 15 and 16A-16C.

Once a color probe 1304 is connected to a respective color injection port 1302, colorant may be injected from the probe, through the port and into: (1) a location that is substantially at a centered position of the polymer stream within the static mixing assembly 208; (2) a location proximate to an inside wall of the housing 702 of the static mixing assembly 208; and/or (3) any other suitable location. Injecting the colorant into the center of the polymer stream may result in more uniform mixing, while injecting the colorant into the polymer stream proximate to a wall of the static mixing assembly's housing 702 may yield more distinct tonal color effects in the resulting colored polymer stream and corresponding BCF product.

FIG. 13 shows three pairs of color injection assemblies 1302a-n positioned in three different locations along the length of the static mixing assembly 208, and four individual color injection assemblies 1302c-1302f. It should be appreciated that any number of color injection assemblies 1302a-n may be used at each respective distance along the length of the static mixing assembly 208, and that groups of one or more color injection assemblies 1302a-n may be positioned at any respective distance along the length of the static mixing assembly 208 without departing from the scope of this disclosure. In particular embodiments, one or more color injection ports are positioned between each of at least 2, 3, 4, 5, 6, 7, or 8 consecutive respective adjacent pairs of mixing elements within the mixing assembly.

For example, while the one or more color injection assemblies 1302 are shown in pairs at each location, various embodiments may utilize only a single color injection assembly 1302 at each location, or may alternatively utilize more than two color injection ports 1302 at each location along the length of the static mixing assembly 208. According to an alternative embodiment, the positioning of the one or more color injection assemblies 1302 around the circumference of the static mixing assembly 208 may differ. For example, a first color injection port 1302a may be positioned on a top side (i.e., at the zero degree location when viewing the circular cross-section) of the static mixing assembly 208, while a second color injection assembly 1302b that is located downstream along the length of the static mixing assembly 208 may be positioned on the right side (i.e., at the 90 degree location when viewing the circular cross-section) of the static mixing assembly 208. The various radial positioning around the circumference of the static mixing assembly 208 may yield different tonal color effects in the colored polymer stream exiting the static mixing assembly 208 if the colorant is injected within the polymer stream at a location other than centrally (i.e., proximate to the wall of the housing 702).

The static mixing assembly 208 shown in FIG. 13 has one or more color injection assemblies 1302a positioned at the upstream end 1308 of the static mixing assembly 208 where the polymer stream enters. As described above, providing colorant at the upstream end 1308 may result in a uniform mix and corresponding uniformly colored polymer stream exiting the downstream end 1310 of the static mixing assembly 208. However, if colorant is added at locations downstream of the upstream end 1308, less mixing of the colorant with the polymer stream may occur, resulting in a tonal color effect. As discussed, colorant added at the one or more color injection assemblies 1302n positioned within 5 to 20 individual static mixing elements from the downstream end 1310 of the static mixing assembly 208, the resulting colored polymer stream is most likely to possess distinct tonal color effects that may be formed into a tonal yarn using one or more spinning machines 212.

According to one embodiment, multiple color probes 1304 (e.g., that are configured to selectively deliver liquid colorant under pressure—e.g., via a suitable pump arrangement, such as any suitable pump arrangement described below) may be utilized simultaneously with multiple corresponding color injection assemblies 1302 at different locations along the length of the static mixing assembly 208 to create tonal color effects with multiple colors. For example, a first color probe 1304 having a first color may be coupled to the color injection assembly 1302b, while a second color probe 1304 having a second color may be coupled to the color injection assembly 1302n. The resulting colored polymer stream may contain tonal color effects with respect to the first color that are more subtle than the tonal color effects associated with the second color that are present in the same colored polymer stream since the polymer stream and the first color mix for a longer period of time than the colored polymer stream (containing a mix with the first color) and the second color.

Alternatively, according to another embodiment, a first color probe 1304 having a first color may be coupled to the color injection assembly 1302n shown on the top side of the static mixing assembly 208, while a second color probe 1304 having a second color may be coupled to the color injection assembly 1302n shown on the bottom side of the static mixing assembly 208. In this embodiment, two different colorants are injected into the polymer stream at different radial locations around the circumference of the static mixing assembly 208. Doing so may allow the polymer stream, the first colorant, and the second colorant to mix for a short length prior to exiting the downstream end 1310 of the static mixing assembly 208 with a unique tonal color effect.

FIG. 14 depicts a high level overview of BCF manufacturing process 1400 for producing and coloring BCF with a tonal color effect, for example, for use in the production of carpet and other products. The process 1400 begins as described above with respect to operations 1 and 2 of FIG. 1 above. Specifically, at operation 1402, PET, PTT, or other polymer flakes are passed through an extruder that melts the flakes and purifies the resulting polymer. At operation 1404, the extruded polymer stream may then be optionally split into a plurality of polymer streams. At operation 1406, PET 220 is added to the polymer stream downstream of the primary extruder 202 if the polymer stream is PTT 200. One or more static mixing assemblies 208 may be used to mix each of the polymer streams at operation 1408. Colorant is added at operation 1410 to the one or more static mixing assemblies 208 through one or more color injection assemblies 1302. The one or more color injection assemblies 1302 that are used for injecting colorant may be selected based on the location of the one or more color injection assemblies 1302 along the length of the one or more static mixing assemblies 208. The locations of the one or more color injection assemblies 1302 determine the amount of mixing of the one or more colorants with the polymer stream within the static mixing assembly 208 and the desired tonal color effect of the resulting BCF product. At operation 1412, each of the polymer streams with the desired tonal color effects are fed into a respective spinning machine 212 to turn the polymer into a tonal filament for use in manufacturing carpets or other products.

Turning now to FIG. 15, an illustrative example of a color injection assembly 1302 will be described. FIG. 15 shows a cross-sectional view of a polymer stream conduit 1504 with a color injection port 1510 and a polymer injection port 1508 for providing liquid colorant and PET 220, respectively, to a polymer stream of PTT 200 (e.g., or for providing liquid colorant to a polymer stream of PET or other suitable polymer or combination of polymers). According to this example, the polymer stream conduit 1504 includes both an inner and outer shell. The PTT 200 stream flows through the inner shell of polymer stream conduit 1504 (e.g., into the page). A heat transfer liquid 1507 flows between the inner shell of 1502 and the outer shell of the polymer stream conduit 1504. An example of a suitable heat transfer liquid 1507 is DOWTHERM “A” from The Dow Chemical Company of Midland, Michigan. The heat transfer liquid 1507 is controlled to keep the PTT 200 within the inner shell 1502 at a proper temperature. According to one example, the PTT 200 flows at approximately 260 ° C. at approximately between about 1000 psi and about 1200 psi.

In particular embodiments, a flange 1512 (e.g., which may be downstream from a pump) or other suitable mechanism may control a flow of heat transfer liquid 1507 between the inner shell 1502 and the outer shell 1504. The polymer injection port 1508 includes a polymer inlet tube 1514 that extends into the interior portion of the polymer stream to deliver PET 220 into the PTT 200. The polymer injection port 1508 will be described in greater detail below with respect to FIGS. 17A-17B.

The right side of FIG. 15 shows an example color injection assembly 1302 configured to engage a color probe 1304 containing the liquid colorant and to position the color probe 1304 within the polymer stream. From this position within the interior portion of the polymer stream, the liquid colorant is released from the outlet end of a stream engagement portion 1516 of the color injection probe 1302 and into the polymer stream. According to one embodiment, the liquid colorant is introduced to the polymer stream at a centered position of the polymer stream that is substantially equidistant from all walls of the polymer stream conduit 1504.

By injecting the liquid colorant into the center of the polymer stream, the efficiency of the mixing within the downstream static mixing assembly is maximized. As stated above, the static mixing assembly 208 of various embodiments may have more than thirty (i.e., thirty six or forty) individual static mixing elements 700, 904. Consequently, due to this relatively large number of individual static mixing elements 700, 904, as well as the orientation of the elements, one would expect a similar and consistent mixing quality of the colorant with the polymer stream regardless of the position within the polymer stream in which the liquid colorant is injected upstream of the static mixing assembly 208. However, tests have shown an unexpected result that the most uniform and consistent mixing quality occurs when the liquid colorant is injected in a centered position within the polymer stream that is substantially equidistant from the walls of the polymer stream conduit 1504. To achieve injection at this centered location, the stream engagement portion 1516 of the color injection port extends into the interior portion of the polymer stream to a position adjacent to the centered position of the polymer stream so that the pressurized colorant exiting the color probe 1304 flows into the pressurized polymer stream at substantially the centered position of the polymer stream conduit 1502.

Similarly, according to one embodiment, the PET 220 is injected into the centered position of the polymer stream that is substantially equidistant from all walls of the polymer stream conduit 1502. In the example shown in FIG. 15, the PET 220 is injected at substantially a same position along a length of a polymer stream conduit encompassing the polymer stream. As seen in this example, the polymer inlet tube 1514 of the polymer injection port 1508 and the stream engagement portion 1516 of the color injection port 1302 are configured on opposing sides of the polymer stream conduit 1502. By injecting the liquid colorant and the PET 220 into the center of the polymer stream at the same location prior to or at the static mixing assembly 208, a relatively short hold up time prevents transesterification of the PET 220 and PTT 200 mixture, while maximizing the efficiency of the color mixing through the static mixing assembly 208.

According to various embodiments, the color injection port 1302 includes a color injector housing 1510 that couples the color injection port 1302 to the polymer stream conduit 1502. The color injector housing 1510 at least partially encompasses a color probe channel 1526 extending through the color injection port 1302. The color probe channel 1526 engages the color probe 1304 and provides a route for the corresponding liquid colorant out of the color probe 1304 and into the polymer stream. The color probe channel 1526 extends from the stream engaging portion 1516, through a pressure blocking mechanism 1524, and through a plunger guide 1522 and corresponding plunger 1520. The plunger 1520 engages the color probe 1304 via threads or other fastening mechanism. The plunger guide 1522 is configured to guide the plunger 1520 and corresponding color probe 1304 through the color injection port 1302 to the stream engaging portion 1516 for delivery of the liquid colorant to the polymer stream.

FIG. 16A shows a side view of the color injection port 1302 in a closed configuration 1602 with the color probe 1304 in a retracted position, according to one embodiment. FIG. 16B shows the same view of the color injection port 1302 in an open configuration 1604 with the color probe 1304 in a deployed position. In the closed configuration 1602, the color injection port 1302 is fluidly decoupled from the polymer stream to prevent the polymer stream at the polymer stream pressure from entering the color injection port 1302.

The pressure blocking mechanism 1524 activates and deactivates to fluidly couple and decouple the color probe channel 1526 of the color injection port 1302 to the polymer stream. When fluidly coupled to the polymer stream, the color injection port 1302 may provide liquid colorant from the color probe 1304 into the polymer stream via the color probe channel 1526. When fluidly decoupled from the polymer stream, the color injection port 1302 is prevented from providing liquid colorant from the color probe 1304 to the polymer stream since the color probe channel 1526 is fluidly disconnected, or blocked, from the polymer stream.

To effectuate this selective coupling and decoupling, the pressure blocking mechanism 1524 may utilize any suitable method for providing a barrier between the polymer stream pressure within the polymer stream conduit 1502 and the pressure on the side of the pressure blocking mechanism 1524 opposite the polymer stream conduit 1502. For example, the pressure blocking mechanism 1524 may utilize a gate, pressure door, or plug that closes over the color probe channel 1526 or otherwise fills the color probe channel 1526 when the color probe 1304 is retracted in order to prevent the polymer stream at the polymer stream pressure from entering the plunger guide 1522.

According to various embodiments, the pressure blocking mechanism 1524 is configured as a cylindrical pressure barrier 1612 that includes a color probe passage 1606. The color probe passage 1606 is substantially similar to the color probe channel 1526 of the color injection port 1302 so that when the color probe passage 1606 is aligned with the color probe channel 1526, the color probe 1304 may be retracted and deployed through the cylindrical pressure barrier 1612 along the length of the color injection port 1302 to transition between closed and open configurations 1602 and 1604, respectively.

FIG. 16A shows the color injection port 1302 in a closed configuration 1602 with the color probe 1304 in a retracted position. FIG. 16B shows the color injection port 1302 in an open configuration 1604 with the plunger 1520 with corresponding color probe 1304 in a deployed configuration. The cylindrical pressure barrier 1612 is rotatable between open and closed positions. A rotation mechanism 1608 is used to rotate the cylindrical pressure barrier 1612. The rotation mechanism 1608 may include a hex nut or other projection or recession that has features that may be engaged by a corresponding tool to mechanically apply torque turn the rotation mechanism 1608 and connected cylindrical pressure barrier 1612. The rotation mechanism 1608 may be manually operated or may be connected to a controller (not shown) that provides control signals to activate or deactivate the rotation mechanism 1608 in response to a feedback loop that provides a color probe replacement instruction due to a low quantity of liquid colorant within the color probe 1304.

In a closed position, as shown in FIG. 16A, the cylindrical pressure barrier 1612 is rotated so that the color probe passage 1606 is not aligned with the color probe channel 1526 and the outer wall of the cylindrical pressure barrier 1612 creates a pressure barrier that blocks the color probe channel 1526 to prevent the polymer stream at the polymer stream pressure from entering the color injection port 1302 beyond the cylindrical pressure barrier 1612. In an open position, as shown in FIG. 16B, the cylindrical pressure barrier 1612 is rotated so that the color probe passage 1606 aligns with the color probe channel 1526 of the color injection port 1302. The color probe 1304 can be seen extending through the color probe passage 1606 of the cylindrical pressure barrier 1612 when the color injection port 1302 is in the open configuration 1604.

The color probe 1304 is engaged with the plunger 1520. The color probe 1304 may be threaded into the plunger 1520 or secured in the plunger 1520 using any suitable fastening mechanism. The plunger 1520 with the color probe 1304 secured within may be moved toward and away from the cylindrical pressure barrier 1612 within the probe guide 1522, in and out of the color probe channel 1526. This movement may be effectuated using a translation mechanism 1610. The translation mechanism 1610 may include threads so that the plunger 1520 and color probe 1304 are screwed into and out of the plunger guide 1522. Alternatively or additionally, the translation mechanism 1610 may include any hydraulic, pneumatic, electro-mechanical, or mechanical mechanisms configured to slide or screw the plunger 1520 and color probe 1304 into and out of the plunger guide 1522. The translation mechanism 1610 may be manually operated or may be connected to a controller (as described above with respect to the rotation mechanism 1608) that provides control signals to activate or deactivate the translation mechanism 1610 in response to a feedback loop that provides a color probe replacement instruction due to a low quantity of liquid colorant within the color probe 1304.

According to various embodiments, the stream engagement portion 1516 of the color injection port 1302 that extends into the polymer stream has features that are configured to maintain, or minimally disrupt, the laminar flow of the polymer stream as it passes. Doing so ensures an accurate delivery of liquid colorant to the centered position of the polymer stream for efficient, uniform mixing through the downstream static mixing assembly 208. FIG. 16C is a cross-sectional view of the stream engaging portion 1516 of the color injection port 1302 taken along the lines shown in FIG. 16A. Specifically, a leading edge flow control device 1620a is attached to a leading edge of the stream engaging portion 1516 of the color injection port 1302, and a trailing edge flow control device 1620b is attached to a leading edge of the stream engaging portion 1516 of the color injection port 1302. Collectively, the leading edge flow control device 1620a and the trailing edge flow control device 1620b are referred to as flow control devices 1620. The flow control devices 1620 may be wedge shaped or may have any desirable airfoil cross-sectional shape that provides for the desired flow characteristics around the stream engaging portion 1516 of the color injection port 1302.

Turning now to FIGS. 17A-17C, front, side, and top views, respectively, of a polymer injection port 1508 for providing PET 220 to a polymer stream of PTT 200 will be discussed. According to various embodiments, the polymer injection port 1508 includes a stream engaging end 1702 encompassing a polymer inlet tube 1514. The stream engaging end 1702 with the polymer inlet tube 1514 extends into the interior portion of the polymer stream to deliver PET 220 into the PTT 200. A gear pump may be operatively connected to a source of PET 220 and the polymer injection port 1508 and may be activated to deliver the PET 220 into the polymer stream. The polymer injection port 1508 may include cooling coils 1708 that may be used to freeze the PET 220 to stop the flow and then heat it up to re-start the flow, should it be necessary to stop the polymer flow for an equipment change or for any reason.

FIG. 18 depicts a high level overview of a process 1800 for introducing a liquid colorant into a polymer stream during manufacturing of a bulked continuous filament, according to various embodiments described herein. The process 1800 begins at operation 1802, where PTT 200 flakes, or other polymer flakes (e.g., PET 220), are passed through an extruder that melts the flakes and purifies the resulting polymer. At operation 1804, the extruded polymer stream may then be optionally split into a plurality of polymer streams. If the polymer stream is a stream of PTT 200, then PET 220 is added downstream of the primary extruder 208 at operation 1806. At operation 1808, a feedback loop determines if the color probe 1304 needs replacing. If not, then the liquid colorant is added to each polymer stream at operation 1810. One or more static mixing assemblies 208 may be used to mix each of the polymer streams at operation 1812. At operation 1814, each of the polymer streams are fed into a respective spinning machine 212 to turn the polymer into a BCF for use in manufacturing carpets or other products.

However, if at operation 1808, it is determined that the color probe 1304 needs replacing, then the process 1800 proceeds to operation 1816 where the transition between open and closed configurations 1604 and 1602, respectively, begins. At operation 1816, the color injection port 1302 is configured in the open configuration 1602, as shown in FIGS. 15 and 16B. To begin the transition to the closed configuration 1604, the color probe 1304 is retracted from the stream engagement portion 1516 and back through the cylindrical pressure barrier 1612. After retracting the color probe 1304 through the cylindrical pressure barrier 1612, at operation 1818, the cylindrical pressure barrier 1612 is rotated as described above to close or block the color probe channel 1526 to prevent backflow of the polymer stream through the color injection port 1302.

At operation 1820, the color probe 1304 may be unscrewed or otherwise removed from the plunger 1520 and replaced with a replacement color probe. At operation 1822, the cylindrical pressure barrier 1612 is rotated to align the color probe passage 1606 with the color probe channel 1526 to open the color injection port 1302 and the replacement color probe is advanced into the polymer stream. The process 1800 then proceeds to operation 1810 and continues as described above.

Operation 5: Use of a Spinning Machine to Turn the Colored Polymer into Filament

Referring back to FIG. 2, after the polymer stream and the added colorant have been sufficiently mixed using the one or more static mixing assemblies 208 (e.g., homogeneously mixed), the resultant colored polymer stream may be fed directly into BCF (or “spinning”) machine 212 that is configured to turn the molten polymer into BCF (See FIG. 2). In particular embodiments, the spinning machine 212 extrudes molten polymer through small holes in a spinneret in order to produce carpet yarn filament from the polymer. In particular embodiments, the molten recycled PET polymer cools after leaving the spinneret. The carpet yarn is then taken up by rollers and ultimately turned into filaments that are used to produce carpet. In various embodiments, the carpet yarn produced by the spinning machine 212 may have a tenacity between about 3 gram-force per unit denier (gf/den) and about 9 gf/den. In particular embodiments, the resulting carpet yarn has a tenacity of at least about 3 gf/den.

In particular embodiments, the spinning machine 212 used in the process described above is the Sytec One spinning machine manufactured by Oerlika Neumag of Neumuenster, Germany. The Sytec One machine may be especially adapted for hard-to-run fibers, such as nylon or solution-dyed fibers, where the filaments are prone to breakage during processing. In various embodiments, the Sytec One machine keeps the runs downstream of the spinneret as straight as possible, uses only one threadline, and is designed to be quick to rethread when there are filament breaks.

Although the example described above describes using the Sytec One spinning machine to produce carpet yarn filament from the polymer, it should be understood that any other suitable spinning machine may be used. Such spinning machines may include, for example, any suitable one-threadline or three-threadline spinning machine made by Oerlika Neumag of Neumuenster, Germany or any other company.

In various embodiments, prior to using the spinning machine 212 to spin the colored melt into filament, the process may utilize one or more color sensors 210 to determine a color of the colored polymer stream. In various embodiments, the one or more color sensors 210 comprises one or more spectrographs configured to separate light shone through the polymer stream into a frequency spectrum to determine the color of the polymer stream. In still other embodiments, the one or more color sensors 210 comprises one or more cameras or other suitable imaging devices configured to determine a color of the resultant polymer stream. In particular embodiments, in response to determining that the color of the polymer stream is a color other than a desired color (e.g., the polymer stream is lighter than desired, darker than desired, a color other than the desired color, etc.) the system may: (1) discard the portion of the stream with the incorrect color; and/or (2) adjust an amount of colorant 204 that is added to the flake and/or the polymer stream upstream in order to adjust a color of the resultant polymer stream. In particular embodiments, adjusting the amount of colorant 204 is executed in a substantially automated manner (e.g., automatically) using the one or more color sensors 210 in a computer-controlled feedback control loop.

Producing a Plurality of Different Colored Fibers Using a Single Primary Extruder

In addition to the single colorant added to a single polymer stream from a primary extruder 202 described above with respect to FIG. 2, the process described herein may be utilized to produce a plurality of different colored filament from a single primary extruder. FIG. 11 depicts a process for producing a plurality of different colored filament from a single primary extruder (e.g., a single MRS extruder) according to a particular embodiment. As may be understood from FIG. 11, the process involves splitting the polymer stream of PTT 200 from the primary extruder 202 into a plurality of individual polymer streams 203a-d (e.g., four individual polymer streams) using any suitable technique. In other embodiments, the process may include splitting the polymer stream from the primary extruder 202 into any suitable number of individual polymer streams (e.g., two individual polymer streams, three individual polymer streams, four individual polymer streams, five individual polymer streams, six individual polymer streams, seven individual polymer streams, eight individual polymer streams, etc.)

As shown in this Figure, a colorant (e.g., Colorant A-D 204a-d) is added to each individual polymer stream, for example, using a respective extruder 206a-d as described above. For example, Colorant C 204 is added to individual polymer stream 203c using extruder 206c. In addition, PET 220 (e.g., PET 220a-d) is added to each individual polymer stream at secondary extruders 206a-d, as described above.

Once the respective Colorant A-D 204a-d and PET 220a-d has been added to the respective individual polymer stream 203a-d, each individual polymer stream 203a-d with added Colorant A-D 204a-d and PET 220a-d is substantially uniformly mixed using respective one or more static mixing assemblies 208a-d. For example, once Colorant D 204d and PET 220d has been added to individual polymer stream 203d, the resultant colorant/PET/PTT mixture passes through the one or more static mixing assemblies 208d to mix the Colorant D 204d, the PET 220d, and the individual polymer stream 203d (e.g., to substantial homogeneity). Following mixture by the one or more static mixing assemblies 208a-d, the resultant respective colored polymer streams are spun into filament using respective spinning machines 212a-d.

In various embodiments, it may be important to monitor the output of the extruder to determine a throughput of each individual polymer stream 203a-d. In such embodiments, monitoring throughput may ensure that each individual polymer stream 203a-d has the proper color letdown ratio in order to add a proper amount of Colorant A-D 204a-d to achieve a desired color of BCF.

As may be understood from FIG. 11, splitting extruded polymer from a primary extruder 202 into a plurality of polymer streams 203a-d prior to the addition of colorant may enable the production of a plurality of colored filament using a single primary extruder 202. Furthermore, by using a plurality of different colorants and extruders downstream of the primary extruder 202, the process may facilitate a reduction in waste when changing a colorant used. For example, when using a single extruder in which color is added upstream of the extruder, there is waste associated with changing over a color package in that the extruder must run sufficiently long between changes to ensure that all of the previous color has cleared the extruder (e.g., such that none of the previous color will remain and mix with the new color). In some embodiments, the wasted filament as a result of a switch in color may include up to several thousand pounds of filament (e.g., up to 4000 pounds). Using a smaller secondary extruder 206a-d to introduce colorant to the various individual polymer streams 203a-d downstream from the primary extruder 202 may reduce (e.g., substantially reduce) the amount of waste associated with a changeover of colorant (e.g., to below about 100 pounds per changeover). Moreover, adding PET 220 at the secondary extruders, at the static mixing assemblies, or within the static mixing assemblies significantly shortens the hold up time, which improves the characteristics of the mixed polymer stream prior to spinning the polymer mixture into BCF.

Alternative Embodiments

Various embodiments of a process for producing various colored bulked continuous filament may include features that vary from or are in addition to those described above. Exemplary alternative embodiments are described below.

Addition of Liquid Colorant to Polymer Stream Using Pump

FIG. 12 depicts an alternative process flow for that, in many respects is similar to the process flow shown in FIG. 11. In the embodiment shown in FIG. 12, however, liquid colorant 204a-d is added to the individual polymer streams 203a-d using a pump 214a-d rather than an extruder. In various embodiments, using a liquid colorant may have the benefit of additional cost saving due to not having to use any additional secondary extruders (e.g., which may have a greater initial cost outlay than a pump, greater running costs than a pump, etc.). In particular embodiments in which a pump 214a-d is used to inject the liquid colorant 214a-d into the individual polymer streams 203a-d, the process may further include exchanging a hose used to connect the pump 214a-d to the individual polymer streams 203a-d when exchanging a particular liquid colorant (e.g., liquid colorant 204a) for a different liquid colorant (e.g., a liquid colorant of a different color). By exchanging the hose when exchanging colorants, waste may further be reduced in that the replacement hose is pre-purged of any residual colorant of the previous color. The color injection ports 1302 described above with respect to FIGS. 15 and 16A-16C may be utilized in the embodiments shown here in FIG. 11. Moreover, this example also shows the addition of PET 220a-d using pumps 224a-d. The polymer injection ports 1508 described above with respect to FIGS. 15 and 17A-17C may be utilized to inject PET 220a-d in this example.

Conclusion

Many modifications and other embodiments of the disclosure will come to mind to one skilled in the art to which this disclosure pertains having the benefit of the teachings presented in the foregoing descriptions and the associated drawings. In addition, it should be understood that various embodiments may omit any of the steps described above or add additional steps. Furthermore, any numerical ranges described herein are intended to capture every integer and fractional value within the described range (e.g., every rational number value within the described range).

For example, it should be understood that a range describing a letdown ration of between about two percent and about eight percent is intended to capture and disclose every rational number value percentage between two percent and eight percent (e.g., 2%, 3%, 4%, 5%, 6%, 7%, 8%, 2.1%, 2.01%, 2.001% . . . 7.999% and so on). Additionally, terms such as ‘about’, ‘substantially’, etc., when used to modify structural descriptions or numerical values are intended to capture the stated shape, value, etc. as well as account for slight variations as a result of, for example, manufacturing tolerances. For example, the term ‘substantially rectangular’ is intended to describe shapes that are both exactly rectangular (e.g., have four sides that meet at ninety degree angles) as well as shapes that are not quite exactly rectangular (e.g., shapes having four sides that meet at an angle in an acceptable tolerance of ninety degrees, such as 90° +/−4°)

In light of the above, it is to be understood that the disclosure is not to be limited to the specific embodiments disclosed and that modifications and other embodiments are intended to be included within the scope of the appended claims. Although specific terms are employed herein, they are used in a generic and descriptive sense only and not for the purposes of limitation.

Claims

1. A method of introducing a liquid colorant into a polymer stream during manufacturing of a bulked continuous carpet filament, the method comprising: providing the polymer stream at a polymer stream pressure; andproviding a color injection port configured to engage a color probe comprising the liquid colorant,wherein the color injection port is further configured to position the color probe within the polymer stream for injection of the liquid colorant and to retract the color probe from the polymer stream for removal and replacement of the color probe while maintaining the polymer stream at the polymer stream pressure.

2. The method of claim 1, wherein providing the color injection port comprises providing the color injection port downstream of a primary extruder and upstream of a static mixing assembly such that the liquid colorant is introduced to the polymer stream upstream of the static mixing assembly.

3. The method of claim 2, wherein providing the color injection port comprises providing the color injection port within a secondary extruder that is positioned downstream of the primary extruder and upstream of the static mixing assembly.

4. The method of claim 1, wherein the color injection port is configured to position the color probe such that the liquid colorant is introduced to the polymer stream at a centered position of the polymer stream that is substantially equidistant from all walls of a polymer stream conduit encompassing the polymer stream.

5. The method of claim 4, further comprising: retracting the color probe from the centered position of the polymer stream to a retracted position; andfluidly decoupling the color injection port from the polymer stream to prevent the polymer stream at the polymer stream pressure from entering the color injection port when the color injection port is configured in a closed configuration.

6. The method of claim 5, further comprising: removing the color probe from the color injection port while the polymer stream is maintained at the polymer stream pressure;replacing the color probe with a replacement color probe;transitioning to an open configuration by fluidly coupling the color injection port to the polymer stream while the polymer stream is maintained at the polymer stream pressure; andrepositioning the replacement color probe from the retracted position to the centered position of the polymer stream.

7. The method of claim 5, wherein retracting the color probe from the centered position of the polymer stream to the retracted position comprises unscrewing the color probe from a color probe channel extending through the color injection port.

8. The method of claim 5, wherein fluidly decoupling the color injection port from the polymer stream to prevent the polymer stream at the polymer stream pressure from entering the color injection port comprises: blocking a color probe channel extending through the color injection port to the polymer stream such that the polymer stream at the polymer stream pressure is prevented from flowing through the color injection port via the color probe channel.

9. The method of claim 8, wherein blocking the color probe channel comprises rotating a cylindrical pressure barrier to a closed position, the cylindrical pressure barrier having a color probe passage configurable to align with the color probe channel when the cylindrical pressure barrier is in an open position that allows the color probe to extend through the cylindrical pressure barrier to the polymer stream, and configurable to block the color probe channel when the cylindrical pressure barrier is in the closed position to prevent the polymer stream from entering the color injection port.

10. The method of claim 1, wherein the color injection port comprises: a pressure blocking mechanism configured to fluidly decouple the color injection port from the polymer stream while the polymer stream is maintained at the polymer stream pressure; anda color probe channel configured to route the color probe from a retracted position, through the pressure blocking mechanism, to the position within the polymer stream.

11. The method of claim 10, wherein the pressure blocking mechanism comprises: a cylindrical pressure barrier having a color probe passage configurable to align with the color probe channel when the cylindrical pressure barrier is in an open position that allows the color probe to extend through the cylindrical pressure barrier to the polymer stream, and configurable to block the color probe channel when the cylindrical pressure barrier is in a closed position to prevent the polymer stream from entering the color injection port.

12. The method of claim 11, wherein the cylindrical pressure barrier is rotatable between the open and the closed positions.

13. A system for introducing a liquid colorant into a polymer stream during manufacturing of a bulked continuous carpet filament, the system comprising: a color injection port housing of a color injection port configured for mechanical coupling to a polymer stream conduit of a bulked continuous carpet filament manufacturing system, the polymer stream conduit encompassing the polymer stream;a stream engaging portion of the color injection port configured to extend into the polymer stream and to position the color probe such that the liquid colorant is introduced to the polymer stream within an interior portion of the polymer stream;a plunger configured to engage a color probe having the liquid colorant;a plunger guide configured to guide the plunger and corresponding color probe through the stream engaging portion to deliver the liquid colorant into the interior portion of the polymer stream;a color probe channel extending from an outlet end of the stream engaging portion of the color injection port through the plunger guide; anda pressure blocking mechanism configured to fluidly decouple the color probe channel from the polymer stream while the polymer stream is maintained at a polymer stream pressure.

14. The system of claim 13, wherein the stream engaging portion comprises a leading edge flow control device configured to maintain laminar flow of the polymer stream over the leading edge of the stream engaging portion of the color injection port.

15. The system of claim 14, wherein the stream engaging portion further comprises a trailing edge flow control device configured to maintain laminar flow of the polymer stream over the trailing edge of the stream engaging portion of the color injection port.

16. The system of claim 13, wherein the interior portion of the polymer stream comprises a centered position of the polymer stream that is substantially equidistant from all walls of a polymer stream conduit encompassing the polymer stream.

17. The system of claim 13, wherein the plunger and the plunger guide are configured with corresponding threads such that the plunger and color probe are configured to screw into the color probe channel toward the outlet end of the stream engaging portion of the color injection port to position the color probe for delivery of the liquid colorant into the polymer stream, and configured to unscrew out of the color probe channel away from the outlet end of the stream engaging portion of the color injection port to retract the color probe for removal and replacement.

18. The system of claim 13, wherein the plunger is configured to slide within the plunger guide such that the plunger and the color probe are configured to be pushed toward the outlet end of the stream engaging portion of the color injection port to position the color probe for delivery of the liquid colorant into the polymer stream, and configured to be pulled out of the color probe channel away from the outlet end of the stream engaging portion of the color injection port to retract the color probe for removal and replacement.

19. The system of claim 13, wherein the pressure blocking mechanism comprises a cylindrical pressure barrier having a color probe passage configurable to align with the color probe channel when the cylindrical pressure barrier is in an open position that allows the color probe to extend through the cylindrical pressure barrier to the polymer stream, and configurable to block the color probe channel when the cylindrical pressure barrier is in a closed position to prevent the polymer stream from entering the color injection port.

20. The system of claim 19, wherein the cylindrical pressure barrier is rotatable between the open and the closed positions.

21. The system of claim 13, further comprising: an extruder fluidly coupled to the polymer stream conduit upstream of the color injection housing and configured to melt polymer into the polymer stream at the polymer stream pressure;one or more static mixers positioned downstream of the extruder and fluidly coupled to the extruder to receive the polymer stream and the liquid colorant and to create a colored polymer stream; andone or more spinning machines positioned downstream of the one or more static mixers and fluidly coupled to the one or more static mixers to receive the colored polymer stream, the one or more spinning machines configured to form the colored polymer stream into bulked continuous carpet filament.

22. A method of introducing a liquid colorant into a polymer stream during manufacturing of a bulked continuous carpet filament, the method comprising: providing the polymer stream at a polymer stream pressure from an extruder;positioning a color probe within the polymer stream at the polymer stream pressure;injecting the liquid colorant from the color probe into the polymer stream upstream of or along a length of a static mixing assembly; andproviding a means for removing the color probe from the polymer stream, replacing the color probe with a replacement color probe, and positioning the replacement color probe within the polymer stream while maintaining the polymer stream flowing at the polymer stream pressure.

23. The method of claim 22, wherein positioning the color probe within the polymer stream at the polymer stream pressure comprises advancing the color probe through an outlet end of a stream engaging portion of a color injection port.

24. The method of claim 23, wherein advancing the color probe comprises screwing a plunger engaged with the color probe into a plunger guide having a color probe channel extending through the outlet end of the stream engaging portion of the color injection port.

25. The method of claim 23, wherein advancing the color probe comprises sliding a plunger engaged with the color probe through a plunger guide and through the outlet end of the stream engaging portion of the color injection port.

26. The method of claim 25, wherein sliding the plunger comprises utilizing a hydraulic or electro-mechanical system to control movement of the plunger.

27. The method of claim 22, wherein providing the means for removing the color probe from the polymer stream, replacing the color probe with the replacement color probe, and positioning the replacement color probe within the polymer stream while maintaining the polymer stream flowing at the polymer stream pressure comprises providing a color injection port, the color injection port comprising: a color injection port housing configured for mechanical coupling to a polymer stream conduit of a bulked continuous carpet filament manufacturing system, the polymer stream conduit encompassing the polymer stream;a stream engaging portion configured to extend into the polymer stream and to position the color probe such that the liquid colorant is introduced to the polymer stream within an interior portion of the polymer stream;a plunger configured to engage a color probe having the liquid colorant;a plunger guide configured to guide the plunger and corresponding color probe through the stream engaging portion to deliver the liquid colorant into the interior portion of the polymer stream;a color probe channel extending from an outlet end of the stream engaging portion of the color injection port through the plunger guide; anda pressure blocking mechanism configured to fluidly decouple the color probe channel from the polymer stream while the polymer stream is maintained at a polymer stream pressure.

28. The method of claim 27, wherein the stream engaging portion comprises a leading edge flow control device configured to maintain laminar flow of the polymer stream over the leading edge of the stream engaging portion of the color injection port and a trailing edge flow control device configured to maintain laminar flow of the polymer stream over the trailing edge of the stream engaging portion of the color injection port.

29. The method of claim 27, wherein the pressure blocking mechanism comprises a cylindrical pressure barrier having a color probe passage configurable to align with the color probe channel when the cylindrical pressure barrier is in an open position that allows the color probe to extend through the cylindrical pressure barrier to the polymer stream, and configurable to block the color probe channel when the cylindrical pressure barrier is in a closed position to prevent the polymer stream from entering the color injection port.

30. The method of claim 27, wherein the cylindrical pressure barrier is rotatable between the open and the closed positions.