Process of making preform articles and polypropylene molded containers from preform articles using injection stretch blow molding techniques

Abstract

The two stage production of clear, low-haze, injection stretch blow molded polypropylene container articles is disclosed. In the first processing stage, a preform article is manufactured on an injection molding machine. In a second and subsequent step, which may occur remotely from apparatus used in the first step, the preform article is heated and stretch blown into a container. The process may employ the selection of processing parameters to produce preform articles that facilitate stretch blow molding at relatively high rates of speed, while still maintaining an appropriate polypropylene polymer morphology that results in clear, low haze containers.

Description

FIELD OF THE INVENTION

This invention relates to production of two-stage injection stretch blow molded polypropylene articles by forming a preform article and then forming a container from the preform article.

BACKGROUND OF THE INVENTION

Injection stretch blow molding is a process of producing thermoplastic articles, such as liquid containers. This process involves the initial production of a preform articles by injection molding. Then, the preform article that after reheating is subjected to stretching and gas pressure to expand (blow) the preform article against a mold surface to form a container.

There are several different processes that employ stretch blow molding. A first type is a single stage process in which a preform is made on a machine and allowed to cool somewhat to a predetermined blow molding temperature. While still at this elevated temperature, the preform is stretch blow molded into a container on the same machine, as part of a single manufacturing procedure. This is a one step or so-called “single stage” manufacturing procedure. In a typical single stage blow molding process for polypropylene, the temperature of the preform is cooled (reduced) following preform formation from about 230° C. to about 120-140° C. The preform is not returned to ambient temperature, but instead is blown to a container while at about 120 to 140° C.

Another type of process is a two stage process. In a two stage process, preforms first are formed in an injection machine. Then, preforms are cooled to ambient temperature. In some cases, preforms are shipped from one location to another (or from one company to another) prior to stretch blowing the preforms into containers. In the second stage of the two-stage process, preforms are heated from an initial ambient temperature to an elevated temperature for stretch blowing on a molding machine to form a container. The injection machine and the molding machine typically are located apart from one another in such a two stage procedure. Two stage manufacturing processes are sometimes referred to as “reheat stretch blow molding” (RSBM) processes, because preform articles formed in the first stage are subsequently reheated during the second stage of manufacture to form finished containers.

Two stage container manufacture is comprised of: (1) injection and cooling of a preform to ambient temperature, followed by (2) stretch blow molding to form a container. Two stage manufacturing reveals certain advantages over single stage processes. For example, preform articles are smaller and more compact than containers. Therefore, it is easier and less costly to transport large numbers of preform articles, as compared to transporting large numbers of containers. This fact encourages producers to make preform articles in one location, and manufacture containers in a second location, reducing overall production costs. Thus, one advantage of two stage container manufacture is that it facilitates separate optimization of each stage of manufacturing. Furthermore, it is recognized that the two stage process is more productive and provides more opportunities for cost savings for large volume applications.

It is common, therefore, for a two-stage process to be used in applications for which large volumes of containers are to be made. Thus, a preform may be shipped to a location at which the finished containers will be employed in the marketplace. Then, in that instance, actual shipping costs for completed containers will be greatly reduced. The explanation for this is that the shipping costs for fully blown containers are significantly greater than shipping costs for preforms, which are much smaller and more compact. Thus, two-stage processes are used commonly for large volume product applications such as drink bottles, soda bottles, water bottles and the like. On the other hand, it is common in the industry for one stage processes to be used for bottles which are used commercially in much smaller volumes.

Stretch blown thermoplastic articles formed of polyethylene terephthalate (PET) are common in the industry. Such polyesters provide highly transparent and aesthetically pleasing container articles. PET bottle production has enjoyed tremendous success in the last twenty years. However, there is a continuing drive in the industry to reduce costs while still providing containers of suitable quality and clarity. Overall production cost for containers is a function of many factors, including raw material cost and also manufacturing speed or efficiency.

In the industry, it is known to make containers from polypropylene. Polypropylene in general is a lower cost raw material as compared to PET. However, polypropylene has not significantly replaced PET as the material of choice for drink bottle manufacturing. One reason that polypropylene has not replaced PET as the material of choice, given its lower overall raw material costs, is that the injection and blow molding cycle time for polypropylene has been excessively long. The long cycle time for preform and bottle production drives up the cost for using polypropylene as compared to PET for container manufacture.

Productivity for polypropylene preform production in conventional processes is low in part because of the undesirably high preform thickness and the use of thermal gates. This is a surprising and unexpected discovery of the invention, that is, a process of achieving suitable container structure and morphology by reducing preform thickness.

In the past, conventional processes have employed a rapid injection rate. It has been mainly the long cooling time that has caused the cycle time for polypropylene preforms to be cost prohibitive. Using a relatively fast injection rate (could still be a short cycle-time) for thin walled preforms unexpectedly can lead to bottles having low clarity. High injection rates in conventional prior art preform manufacture sometimes have adversely affected the orientation of the crystal structure in the preform, which induces undesirable haze in the final container. To produce containers with sufficient clarity, it has been common to use relatively long cycle times (for preforms and containers) when employing polypropylene.

There has been a long felt need in the industry for a process of making polypropylene containers on existing PET manufacturing equipment that is already deployed in the industry. Currently known methods of injection stretch blow molding PET preforms have generally not been successfully employed for polypropylene container manufacture.

The shape and thickness of preforms will determine their suitability for container manufacture and the speed at which containers may be stretch molded from such preforms. It has been common in conventional polypropylene processes to employ polypropylene preforms having fairly thick walls. However, thick preform walls reduce the processing speeds that can be achieved. Thick-walled preforms must be cooled longer before removal from a preform mold, thus undesirably increasing processing time in preform manufacture.

U.S. Pat. No. 4,357,288 to Oas et al. discloses a method of manufacture of biaxially oriented polyolefin bottles. The injection rate for production of preforms, however, is relatively slow. This patent describes an injection rate of polypropylene to fill a mold cavity which uses an injection time of about 3 to 10 seconds to fill the mold cavity. Examples of the Oas patent disclosure recite a machine cycle of about 7 seconds, which corresponds to a container production of about 500 containers per hour.

Several prior art references are directed to single stage bottle manufacturing processes, or extrusion-type processes. For example, European patent application

0 151 741 A2 to Ueki et. al. (Mitsui Toatsu Chemicals) is directed to single stage manufacturing of containers or bottles. EP 0 309 138 A2 (Exxon) teaches the use of polypropylene to form containers. This Exxon patent disclosure is directed to one stage preform/container manufacturing processes.

An additional publication, WO03/0353368 to Richards et al. (Pechiney Emballage Flexible Europe) is directed to the two stage production of multilayer containers from polypropylene. An additional barrier layer of EVOH is provided in addition to the polypropylene layer. However, this patent disclosure teaches the use of a melt flow index that is relatively low, resulting in a relatively viscous polypropylene resin. Viscous resins are not easily adapted to rapid injection rates in the manufacture of preforms. This reduces overall productivity and manufacturing efficiency.

Yet another publication, WO 95/11791 to Gittner et al, (Bekum Maschinenfabriken GMBH) is directed to a two stage process for container manufacture using polypropylene. This process employs an injection cavity fill rate during manufacture of the preform of about 3-5 grams per second. It is believed that the process cannot reliably form polypropylene containers at a container production rate of more than about 900 containers per cavity per hour.

Until the development of this invention, many attempts to injection stretch blow mold polypropylene have been commercially undesirable. This has been believed to be due in part to a relatively slow production speed for such polypropylene articles at acceptable container haze levels. In addition, it was generally believed that special stretch blow molding machines equipped with longer re-heating ovens were required to reliably produce polypropylene containers.

A disadvantage of polypropylene containers has been the inability to make containers of high clarity (i.e. low haze) at a high rate of speed. For example, it has been known to make relatively clear polypropylene containers having a percentage haze value of about 1-1.5 percent haze. However, conventional methods for making polypropylene containers having such low levels of haze have been relatively slow. Slow processes are not economically viable in the marketplace. It is a significant and difficult challenge to develop a process that will facilitate increased stretch molding speed while not sacrificing clarity of the resulting container.

There has been a long felt need in the industry of container manufacturing to provide polypropylene materials, preforms, and container articles in a process that will afford a cost-effective manufacture of low-haze, high clarity products. A process of employing polypropylene in a manner that will result in highly efficient preform and container production at a minimum cost with a fast cycle time is very desirable.

BRIEF DESCRIPTION OF THE DRAWINGS

The invention will now be described by way of example with reference to the drawings:

FIG. 1 shows a typical polypropylene container that may be manufactured according to the process of the invention;

FIG. 2A is a schematic flow diagram showing the processing steps employed in the first stage of the two stage process, which relates to injection manufacture of preform articles;

FIG. 2B illustrates processing steps in the second stage of manufacturing in accord with the invention, wherein a preform article is stretch blow molded to form a container;

FIG. 3 is a side view of a conventional thick-walled preform article;

FIG. 3A shows a side cross-sectional view of the conventional preform article of FIG. 3;

FIGS. 3B and 3C show a first embodiment of a relatively thin walled preform with an external profile that may be employed in the invention;

FIG. 4 shows a side view of a second preform that may be used in the invention, i.e. a relatively thin-walled preform article according to the practice of the invention, in which the preform article optionally may have a profile on the inside rather than the outside of the preform article structure;

FIG. 4A shows a cross-sectional view of the thin-walled preform article of FIG. 4;

FIG. 5 is a longitudinal sectional view of an injection molding assembly for the production of a preform article;

FIG. 6 is an illustration of stage two of the manufacturing process, showing a vertical cross-sectional view of stretch blow mold apparatus that is used to produce the containers from a perform, in this view showing a start up position with the preform article in place;

FIG. 7 is a view of the apparatus of FIG. 6 showing the mold closed on the preform article; and

FIG. 8 shows a fully blown container with a stretch rod and swage in a down position with the container decompressing in the mold;

FIG. 9 shows an ISBM (injection stretch blow molding) critical filling rate model showing in three dimensions the maximum filling rate for a given set of MFI and thickness values that may be employed;

FIG. 10 is a graph showing, for given critical filling rates (i.e. 5, 10, 15, 20, etc.) the values of MFI and thickness of preform that would correspond, according to one set of data produced in connection with the invention;

FIG. 11 shows, for a given preform wall thickness (2 mm, 3 mm, 4 mm), corresponding MFI values and corresponding critical filling rate values; and

FIG. 12 is a graph showing percent haze versus mold fill time, indicating the effect of pre-blowing time on haze of the container ultimately formed from the preform article.

DETAILED DESCRIPTION OF THE INVENTION

Reference now will be made to the embodiments of the invention, one or more examples of which are set forth below. Each example is provided by way of explanation of the invention, not as a limitation of the invention. In fact, it will be apparent to those skilled in the art that various modifications and variations can be made in this invention without departing from the scope or spirit of the invention.

A two-stage process of injection stretch blow molding polypropylene to form a container is disclosed in the practice of the invention. A first stage of this process comprises forming a preform article. A second subsequent stage comprises reheating and blow molding the preform article to form a container. The invention is directed to both preform articles and containers, in addition to the specific method or process for forming these products. Surprisingly beneficial results have been achieved in the practice of the invention.

In the first stage of forming a preform article, a process is provided having at least the following steps. First, a chemical composition comprising at least in part polypropylene is provided. This chemical composition provides a melt flow index in the range of between about 6 and about 50 grams/10 minutes, according to ASTM D 1238 at 230 degrees C./2.16 kg.

Further, the chemical composition is injected into a mold at a fill rate of greater than about 5 grams of chemical composition per second. This injection may be made through an orifice or gate, as further described herein. A preform article is formed in a mold. The preform article is removed from the mold. The preform article includes a closed end adapted for subsequent second stage reheating and stretch blow molding. The closed end may be integral with a side wall. The side wall of the preform provides a thickness of less than about 3.5 mm, in one aspect of the invention.

Processing parameters are employed in the practice of the invention to produce preform articles that facilitate fast and efficient stretch blow molding to produce containers having a desirably low haze. The melt flow index (MFI) of the polypropylene chemical compositions (i.e. resins) will be tuned to the injection speed of resin in molding the preform article, the thickness and structure of the preform article, and the proper selection of injection gate diameter during such the preform production stage. Each of these factors are important to the successful production of desirable low-haze container articles. Improved containers, preforms, and processing conditions are within the scope of this invention.

The invention has overcome limitations in the art, in part by the unexpected discovery that processing parameters may be established to impart necessary conditions and benefits to form superior polypropylene-based preforms. This invention facilitates efficient and cost-effective production of clear, low haze polypropylene articles from preforms using injection to make a preform, followed in some instances by stretch blow molding to form a container.

It is highly desirable to improve the speed of production and reduce the level of haze in the thickest regions of the resultant container articles as well. Nucleating agents may be employed in the practice of the invention, but are not always necessary. For injection stretch blow-molded bottles, as one example, the neck and the bottom are generally the most difficult areas to clarify due to the thickness of such regions. In particular, the aesthetic qualities of neck areas can be compromised if the appearance is too hazy or cloudy.

The advantages of the process disclosed herein comprise, among other things, appropriate selection of melt flow polypropylene resins, appropriate selection of nucleating and clarifying agents, appropriate thickness of performs, appropriate rate or speed of injecting the resin for preform production, and also perhaps the appropriate gate width during preform production. Surprisingly, it has been found that there are ranges for each of these criteria which cause stretch blow molded articles to be produced at high rates with superior clarity.

Polypropylene has long been known to exist in several forms, and essentially any known form could be used in the practice of the invention. Thus, the invention is not limited to any particular type of polypropylene. Isotactic propylene (iPP) may be described as having the methyl groups attached to the tertiary carbon atoms of successive monomeric units on the same side of a hypothetical plane through the polymer chain, whereas syndiotactic polypropylene (sPP) generally may be described as having the methyl groups attached on alternating sides of the polymer chain.

Additionally, container articles produced in accordance with the criteria noted above exhibit specific haze to thickness ratios, and such is within the scope of the present invention. The invention provides a vast improvement in polypropylene injection stretch blow-molded article technology whereby efficient methods of producing very clear articles is accorded as proper replacements for previous PET types.

The practice of the invention makes it possible to provide injection stretch blow-molded polypropylene articles that may be produced at very high rates and exhibit substantially uniform clarity levels. The invention may provide polypropylene preforms that facilitate production of very low haze container articles with injection stretch blow molding in a very efficient manner. One application of the invention provides improved containers, wherein such containers (or bottles) exhibit low haze levels.

Optional Nucleating Agents

An effective clarifying agent, that also functions as a nucleator, for polypropylene is 1,3-O-2,4-bis(3,4-dimethylbenzylidene) sorbitol (hereinafter DMDBS), available from Milliken & Company under the trade name Millad® 3988. Such a compound provides highly effective haze reductions within polypropylenes with concomitant low taste and odor problems. Disubstituted DBS compounds are broadly described in U.S. Pat. Nos. 5,049,605 and 5,135,975 to Rekers. As it is, in terms of providing excellent clarity, particularly within the neck and bottom regions of target injection stretch blow-molded polypropylene bottle articles within this invention, DMDBS is a useful compound for such a result.

An effective thermoplastic nucleator in terms of high crystallization temperatures is available from Milliken & Company using the trade name HPN-68™. Other like thermoplastic nucleating compounds that may be employed in the practice of the invention is disclosed in U.S. Pat. Nos. 6,465,551 and 6,534,574. The HPN-68™ compound is disodium bicyclo[2.2.1]heptanedicarboxylate. The ability to provide highly effective crystallization, or, in this specific situation, control targeted levels of crystallization within polypropylene preforms prior to injection stretch blow molding sometimes is facilitated by utilization of such a nucleating agent. Low amounts of this additive can be provided to produce the desired and intended amorphous-crystalline combination within the target performs.

Other nucleating agents can be employed in the practice of the invention. These include dibenzylidene sorbitol compounds (such as unsubstituted dibenzylidene sorbitol, or DBS, and p-methyidibenzylidene sorbitol, or MDBS), sodium benzoate, talc, and metal salts of cyclic phosphoric esters such as sodium 2,2′-methylene-bis-(4,6-di-tert-butylphenyl) phosphate (from Asahi Denka Kogyo K.K., known as NA-11), and cyclic bis-phenol phosphates (such as NA-21®, also available from Asahi Denka), metal salts (such as calcium) of hexahydrophthalic acid, and, as taught within Patent Cooperation Treaty Application WO 98/29494, to 3M, the unsaturated compound of disodium bicyclo[2.2.1]heptene dicarboxylate. Such compounds all impart relatively high polypropylene crystallization temperatures.

Commercially available products suitable for use in the practice of the present invention include not only Millad® 3988 (3,4-dimethyidibenzylidene sorbitol) mentioned above, but also NA-11® (sodium 2,2-methylene-bis-(4,6, di-tert-butylphenyl)phosphate, available from Asahi Denka Kogyo, and aluminum bis[2,2′-methylene-bis-(4,6-di-tert-butylphenyl)phosphate], known commercially as NA-21®, also available from Asahi.

The following nucleating agents could be used in the practice of the invention: sodium 1,3-O-2,4-bis(4-methylbenzylidene) sorbitol and derivatives thereof: 1,2-cyclohexanedicarboxylate salts and derivatives thereof; aluminum 4-tert-butylbenzonate and derivatives thereof; and metal salts of cyclic phosphoric esters and derivatives thereof.

Nucleating agents, clarifying agents, HHPA and/or bicyclic salts, as further described herein, may be added to polypropylene in an amount from about 0.01 percent to about 10 percent by weight. In most applications, however, less than about 5.0 percent by weight of such nucleating agents are needed. In other applications, such compounds may be added in amounts from about 0.02 to about 3.0 percent. Some applications will benefit from a concentration of about 0.05 to 2.5 percent, to provide beneficial characteristics (1.0% by weight equals about 10,000 ppm).

It may be desirable to include up to 50% or more of an active nucleating agent compound in a master batch, prior to full homogenous mixing, although this is not a restriction or a requirement. Optional additives in addition to the nucleating salt-containing composition may include plasticizers, stabilizers, ultraviolet absorbers, and other similar thermoplastic additives. Other additives also may also be present within this composition, most notably antioxidants, antimicrobial agents (such as silver-based compounds, preferably ion-exchange compounds such as ALPHASAN® brand antimicrobials from Milliken & Company), antistatic compounds, perfumes, chloride scavengers, and the like. Co-additives, along with the nucleating agents, may be present as an admixture in powder, liquid, or in compressed or pelletized form for easy feeding as shown in FIG. 5 herein. The use of dispersing aids may be desirable, such as polyolefin (e.g., polyethylene) waxes, stearate esters of glycerin, montan waxes, and mineral oil.

Polypropylene Compositions

The polypropylene polymers employed in the practice of the invention may include homopolymers (known as HPs), impact or block copolymers (known as ICPs)(combinations of propylene with certain elastomeric additives, such as rubber, and the like), and random copolymers (known as RCPs) made from at least one propylene and one or more ethylenically unsaturated comonomers. Generally, co-monomers, if present, constitute a relatively minor amount, i.e., about 10 percent or less, or about 5 percent or less, of the entire polypropylene, based upon the total weight of the polymer. Such co-monomers may serve to assist in clarity improvement of the polypropylene, or they may function to improve other properties of the polymer. Co-monomer examples include acrylic acid and vinyl acetate, polyethylene, polybutylene, and other like compounds.

Polypropylene provides an average molecular weight of from about 10,000 to about 2,000,000, preferably from about 30,000 to about 300,000, and it may be mixed with additives such as polyethylene, linear low density polyethylene, crystalline ethylenepropylene copolymer, poly(1-butene), 1-hexene, 1-octene, vinyl cyclohexane, and polymethylpentene, as examples. Other polymers that may be added to the base polypropylene for physical, aesthetic, or other reasons, include polyethylene terephthalate, polybutylene terephthalate, and polyamides, among others.

Resin compositions utilized to produce the preform articles and injection stretch blow-molded containers of the invention can be obtained by adding a specific amount of a nucleating agent/clarifying agent directly to the polypropylene, either in dry form or in molten form, and mixing them by any suitable means while in molten form to provide a substantially homogenous formulation. Alternatively, a concentrate containing as much as about 20 percent by weight of a nucleator/clarifier in a polypropylene masterbatch may be prepared and be subsequently mixed with the resin. Furthermore, the desired nucleator/clarifier (and other additives, if desired) may be present in any type of standard polypropylene additive form, including, without limitation, powder, prill, agglomerate, liquid suspension, and the like, particularly comprising dispersion aids such as polyolefin (e.g., polyethylene) waxes, stearate esters of glycerin, waxes, mineral oil, and the like. Essentially any form may be exhibited by such a combination or composition including such combination made from blending, agglomeration, compaction, and/or extrusion. The produced resins are then utilized to form preforms, as noted herein, which are then subsequently utilized to form the desired container articles in an injection stretch blow molding procedure.

Other additives may also be used in the composition of the present invention. It may even be advantageous to premix such additives or similar structures with the nucleating agent to reduce its melting point and thereby enhance dispersion and distribution during melt processing. Such additives are known to those skilled in the art, and include plasticizers (e.g., dioctyl phthalate, dibutyl phthalate, dioctyl sebacate, mineral oil, or dioctyl adipate), transparent coloring agents, lubricants, catalyst neutralizers, antioxidants, light stabilizers, pigments, other nucleating agents, and the like. Some of these additives may provide further beneficial property enhancements, including improved aesthetics, easier processing, and improved stability to processing or end use conditions.

In particular, it is contemplated that certain organoleptic improvement additives be added for the purpose of reducing the migration of degraded benzaldehydes from reaching the surface of the desired article. The term “organoleptic improvement additive” is intended to encompass such compounds and formulations as antioxidants (to prevent degradation of both the polyolefin and possibly the target alditol derivatives present within such polyolefin), acid neutralizers (to prevent the ability of appreciable amounts of residual acids from attacking the alditol derivatives), and benzaldehyde scavengers (such as hydrazides, hydrazines, and the like, to prevent the migration of foul tasting and smelling benzaldehydes to the target polyolefin surface).

High rate production of preforms contributes significantly to the improved efficiency in producing of injection stretch blow-molded articles, in terms of high clarity, acceptable physical properties, and high manufacturing efficiency.

Polypropylene compositions having a melt flow index (MFI) of between about 6 and about 60 are useful in the practice of the invention. Furthermore, MFI values of between about 13 and about 35 are particularly useful in the practice of the invention, as further described below.

An injection speed of the chemical composition (i.e. polypropylene and various additives) into a preform cavity mold at a fill rate of greater than about 5 grams of chemical composition per second has been found to be particularly valuable in the practice of the invention. Table A shows values for various parameters that may be employed in the practice of the invention, as further discussed herein.

In addition to the injection speed of the specific MFI resin, the thickness and design of the target preform is important for a number of reasons. The thickness of such an article should be thin, as compared with the thickness of previously produced polypropylene preforms. This facilitates utilization within prior PET injection stretch blow molding machinery. The side wall thickness of preforms desirably may be less than about 3.5 mm for effective results. In some applications, side wall thickness of between about 1.5 mm and 3.5 is very useful. Some applications may use a thickness of as much as 4.0 mm, as set forth in Table A.

A gate, as further described herein, comprises the opening through which liquid chemical composition (polypropylene and additive mixture) is admitted into the preform mold cavity. The gate diameter employed during preform production is particularly important, and may be related to other processing variables. A wider gate during injection into the mold cavity, coupled with the particular speed or speed range at which the resin is injected, facilitates greater control and influence upon the degree of polymer crystal orientation resulting therefrom. In the practice of the invention, a gate diameter of 1.5 mm may be used. In other applications, a gate diameter of 3.8 mm has been used. Other gate sizes could be used as well, but each factor or factor must be adjusted to account for gate diameter. Gate diameters between about 1.5 mm and 3.8 mm can be advantageously employed in the practice of the invention.

Further Detailed Description of the Drawings

FIG. 1 shows a stretch blow molded polypropylene container that may be manufactured in accordance with the practice of the invention. Container 10 (sometimes referred to herein as a “bottle”) is shown. The container 10 of FIG. 1 has a relatively concave bottom 11, a cylindrical main sidewall 12, a conical upper portion 13, and a thickened externally threaded neck 14 on the convergent end of the upper portion 13. A neck ring 15 provides a physical point of reference, and may be used to carry the container 10 along processing machinery during manufacture and subsequent filling of the container 10.

The container 10 may be of any desired size or shape with sizes of from 0.5 to 4 liters being very useful, for example. The neck 14 usually is rigid to support a pressure retaining screw type cap (not shown). Thus, the neck 14 may be many times the thickness of the sidewall 12. Furthermore, the conical upper portion 13 may be gradually thickened as it approaches neck 14.

Turning now to FIG. 2A, a flow schematic is provided showing the steps in the first stage of a two-stage stretch blow molding process. In the invention, a two stage (two step) procedure is provided for production of containers 10. FIG. 2A shows the first stage of the manufacturing procedure, that is, the injection molding process of preforms production. A chemical composition containing polypropylene is acquired from a source, such as a polypropylene manufacturer. The polypropylene-containing chemical composition may comprise a homopolymer, copolymer or other polymeric composition. Furthermore, the chemical composition (also known as a “resin”) may contain various additives, including (for example) nucleating agents, antioxidants, lubricants, s-scavengers, UV absorbers and the like, as further described herein. The polypropylene chemical composition is provided into an injection machine and heated. The heated chemical composition then is injected at a relatively high rate of speed through a valve or “gate”, and into the mold of the injection machine. A preform article is formed in a mold. The preform article is cooled is and removed from the mold.

FIG. 2B shows a second stage of a two-stage stretch blow molding process. In the second stage, a preform article (which may or may not have been manufactured at a location distant from the stretch blow molding apparatus) is converted to a container 10. A preform article (usually at ambient temperature) is provided in a stretch blow molding machine. Then, the preform article is heated from ambient temperature to an elevated temperature. The elevated temperature employed is also known as the “orientation” temperature, and it is typically in the range of about 120-130° C. for random copolymers.

The inner surface temperature of the preform needs to be sufficiently high to ensure that containers have the best optical properties. This has been found to be one important variable in the stretch blow molding process which sometimes determines whether the container will be transparent or hazy. When the preform article is sufficiently softened, the preform is stretch blow molded into a container 10. The formed container 10 is cooled and removed from the stretch mold apparatus.

Conventional Thick-Walled Preform

FIGS. 3-3A show a thick-walled polypropylene preform having a relatively thick side wall 80 (in this example, the side wall thickness is about 5 mm). The preform article 60 shown in FIG. 3 includes a closed end 62 and an open end 72. Furthermore, a neck 66 is shown, with threads 68 at the base of the neck 66. A main body portion 64 with side wall 80 is shown. It is common for polypropylene-based preforms 60 such as that shown in FIG. 3 to have a side wall 80 having a thickness of about 5 mm, or more.

This preform article 60 happens to also be “stepped out” or tapered at each end, on its exterior profile. Thus, a “profile” is found on the exterior of many preform articles. In many cases, the size of the threads at the open end 72 are fixed, and cannot be subject to variation.

One Type of Preform Article That May be Employed in the Practice of the Invention

FIG. 3B and corresponding FIG. 3C show a first embodiment of a thin walled preform article that may be employed in the practice of the invention. It should be noted that the invention may include the use of “stepped out” preforms with an exterior profile, such as shown in FIGS. 3B/3C so long as the preforms are less than about 3.5 mm in side wall width.

Thus, one discovery of the invention is that thin-walled preforms, in conjunction with processing conditions presented herein, provide surprisingly unexpected results as compared to conventional thick walled preforms. In the FIGS. 3B/3C a preform 90 having thin side wall 91 is shown.

Second Type of Preform Article Employed in the Invention

The geometry of a preform article is important in the manufacturing of containers 10. In the practice of the invention, a preform article 115 having a relatively thin side wall may be employed, as further described herein and as shown in FIGS. 4-4A. The geometry of the preform article 115 of FIG. 3 shows a tapered neck 114, and a main body portion 102 with side walls 101 and 104 that are approximately parallel to each other along their length. Furthermore, a closed end portion 116 tapers from the main body portion 102. Threads 110 are provided adjacent the open end 103 of preform article 115. A transition area 105 represents the tapering region of the side wall 101 into the neck 114.

In FIG. 4, a preform article 115 of the invention is shown in which the outer wall surfaces 109a-b of the preform article are generally parallel and straight, forming a substantially symmetrical tube on its outer dimension from a point near the closed end 116 to a point near the open end 103. The inner wall 108 of the preform 115 is profiled due to a transition zone 105. When blown in stage two of manufacture, the preform article 115 engages a mold so as to make a container 10 of the appropriate geometry.

By “profiled”, it is meant that a given wall has a changing angle or slope which deviates from 180 degrees. Thus, the invention may in some embodiments take advantage of a profiled inner wall 108, as opposed to a profiled exterior wall, as is common in the conventional devices (see FIGS. 3-3A). The use of a profiled inner wall 108 has been found to be a useful feature in application of the preform 115 to container 10 manufacture. One reason for this fact is that it facilitates the use of relatively uniform outer wall dimensions. Thus, preforms 115 can be used that have differing inner wall 108 profile for various container sizes, while still exhibiting a common outer dimension or shape. This is useful in manufacturing, to avoid or minimize tooling and/or machinery changes for each size preform 115 that may be used to make containers 10 of various sizes.

Thus, a relatively uniform outer dimension to the preform articles 115 may provide an advantage that may be realized in the practice of the invention. It should be recognized that the use of a profiled inner wall 108 is not required in the practice of the invention, but is one useful manner of practicing the invention. Thus, preforms having either an exterior profile or an exterior profile may be used in the practice of the invention.

Injection Molding of Preforms

FIG. 5 shows a schematic vertical cross-sectional view of an injection molding machine for making preform articles in a first stage. A preform article 115 may be formed in an injection molding unit 120 having a barrel 121 fed by a hopper 122 and ejecting the melt through a round nose nozzle 123. A chemical composition (i.e. polypropylene-containing pellets or portions, with optional additives or optional nucleating agents, etc) is provided into inlet hopper 122. Barrel 121 rotatably mounts a melting and mixing screw 124 with a non-return valve nose 125. Heater bands 126 may be provided in the barrel 121. Crystalline polypropylene stretch blow mold formulations are fed through the hopper 122 into the barrel 121 where they are advanced by the melting and mixing screw 124 to a molten condition at the valve end 125 whereupon the screw is advanced to the dotted line position where the valve nose 125 will force the molten material through the nozzle orifice 127. Gate 137a received a determined the amount of liquid flow that proceeds into the molding cavity 135. Other similar apparatus could be used to form a preform, which achieves the same or similar result as that shown in FIG. 5.

The apparatus includes a two-part mold 130 with a first core part 131 and a second molding cavity defining part 132. The part 131 has a cylindrical core 133 with a hemispherical end 134. The part 132 has a molding cavity 135 with a hemispherical bottom end 136 fed by a conduit 137. The end wall of the part 132 has a recess 138 receiving the rounded nose of the nozzle 123.

With the apparatus in the position of FIG. 4 the molten plastics material ahead of the valve 125 may be ejected through the orifice 127 by moving the screw rod to the dotted line position as shown in FIG. 5. The molten material will flow through the conduit 137 into the mold cavity 135.

The surface of core 133 and the molding cavity surfaces 135 and 136 typically are polished, but may be treated as well to facilitate the ejection of preforms 115. Steel is a desired metal for manufacture of such mold surfaces 135. Chilled mold temperatures from about 11-20 degrees C. may be employed.

One feature employed when injection molding preform articles 115, as shown in FIG. 5, is the Gate 137a. The gate 137a refers is the opening between the point at which the liquid polypropylene is injected and the actual core 134 of the mold cavity 135. Gate size is a parameter that may vary for different applications. The size of the gate 137a can be important in the manufacture of preformed articles 115. This is because the size of the gate 137a determines the shear forces applied to the molten polypropylene as it is injected into the mold cavity. The size of gate 137a will affect the filing rate. The size of the gate 137a will in some cases determine the rate by at which the chemical composition may be injected, which affects the ultimate clarity of the containers 10 produced by the preformed article 115 in the second stage of the container 10 manufacture (see FIG. 2B).

To improve the economics of making polypropylene preforms, it may be important to inject chemical compositions quickly (shorter preform cycle time) into the mold cavity 135. However, when injecting quickly, the clarity of the container 10 produced may be compromised because of the characteristics imparted to the preform article 115 during such mold fill step. Thus, using a relatively wide or large gate 37a allows one to inject at a faster rate while still achieving the same or sufficient clarity in the final container. In some applications, this is desirable. Gate diameter may vary, depending upon the application. The invention is not limited to any particular gate diameter, but it has been found that diameters between about 1.5 mm and about 3.8 mm are useful, and may be found in equipment in the industry. It may be an advantage in the practice of the invention to be capable of employing gate diameter settings that already are in existence and used on existing commercial PET processing equipment.

The injection rate usually is relatively slow. Cavity filling time is typically about 1 to about 4.5 total seconds to fill mold cavity 135. This corresponds generally to an injection rate greater than about 5 grams/second. In other cases, the rate may be between about 5 and about 22 grams per second. Table A shows various parameters that may be advantageously employed in the practice of the invention.

Upon solidification of the preform article 115 in the mold 130, the mold 130 is opened by withdrawing part 131 (and core 133) from part 132. The preform 115 is stripped from the mold.

Melt Flow Index (MFI)

The melt flow index (MFI), also known as the melt flow rate, is an important factor in the manufacturing of preform articles 115. In general, melt flow index is measured according to American Society of Testing Materials ASTM D-1238. This testing method is a nationally (or internationally) known standard. It is a standard test method for measuring the melt flow rates of thermoplastics. Unless otherwise indicated herein, all references to melt flow index, melt flow rate, MFI, or MFR, refer to measurements according to this industry standard. For polypropylene, measurements are at 230 degrees C., and using 2.16 kg, as per this standard.

In general, the more viscous is a material at a given temperature, the lower will be the MFI value of that material. For example, a given polymer or copolymer composition will have an MFI that is specified by a manufacturer. Thus, each particular type of polypropylene-containing composition to be employed in the practice of the invention will have a given or predetermined MFI. The MFI is also determined and affected by the length of the polymer chains in a given polypropylene composition. The longer the polymeric chains, the more viscous the material. The more viscous the material, the lower the MFI value will be for a given composition.

MFI values are important in determining the speed at which a chemical composition may be fed into an injection mold cavity to form a preform article. This is true because the MFI also will affect the clarity of the final container which is produced from the preform. By clarity, it is meant the degree of haze that will be present in a given container 10 made according to the invention. In general, the higher percentage of haze in the container 10, the less transparent is the container 10 produced in the invention. Higher levels of haze are undesirable.

One unexpected result of the invention is that it has been found that using a given polymeric composition having a predetermined melt flow index, and injecting that composition at a fill rate of greater than about 5 grams per second, a highly desired preform article may be formed. Furthermore, it has been found that the sidewall thickness of the preform is very important in container manufacture. In the practice of the invention, a preform article 115 with a side wall thickness of less than about 3.5 millimeters has proved to be very desirable. This achieves a high productivity of container manufacture while still maintaining a low degree of haze, i.e. a clear container. Cycle time necessary to make a preform article 115 is significantly reduced by using a preform design with a minimum side wall thickness. Hot plastic (polypropylene) is capable of cooling in the preform mold more quickly using a reduced wall thickness for the preform stage. This facilitates faster preform cycle times, thereby increasing the number of preform articles 115 that can be made in a given period of time, increasing manufacturing capacity and efficiency.

Stretch Blow Molding Preform Articles to Form Containers

Stage two (step 2) of manufacture is shown generally in FIGS. 2B, and FIGS. 6-8. A preform article 115 is taken at ambient temperature, and then uniformly heated. The preform article 115 is placed in a stretch blow mold apparatus 140 in a position with its open end 103 resting on a platform 141 on a base 142 surrounding a reciprocal swage 143. The closed end 116 of the preform 115 is shown near the center of FIG. 6. The apparatus freely receives the retracted end of the stretch rod 144 of the apparatus 140. The molding dies 145 of the apparatus 140 are in an opened condition. Threaded neck forming wall portions 146 are shown, as well as tapered cone forming portions 147, cylindrical main body forming portions 148, and concave bottom forming portions 149.

Alternatively, and in some embodiments, it may be that a rotary system is employed to transfer preforms using transfer wheels equipped with grippers into a blow mold cavity. Thus, rotary stretch blow molding equipment is known in the art, and may be applied in the practice of the invention. From the open position of FIG. 6 the apparatus 140 is closed to the position of FIG. 7 with the mold halves 145 coming together and with the swage 143 extended into the open end of the preform 115 so that the neck and thread forming portions 146 of the die can mold the thick neck 114 of the bottle on the preform 115. The projection of the swage 143 into the position of FIG. 7 also moves the stretch rod 144 against the closed end 116 of the preform 115.

From the position of FIG. 7 the apparatus 140 is further activated to eject the stretch rod 144 beyond the swage 143 into closely spaced relation from the bottom forming portion 149 of the dies 145 thereby effecting a stretching of the preform 115 to the full height of the dies. As shown in FIG. 8, the stretch rod 144 and the swage 143 are retracted from the container 10. The gas pressure in the bottle is released, and the dies 45 are separated. A blowing agent is introduced into the preform article 115 forming an axially elongated and hoop stretched balloon in the closed die. The balloon (not shown) is blown into a finished container 10, as shown in FIG. 8, with the polypropylene material biaxially stretched to produce a strong container 10.

Roughness on the inner container 10 surface has a negative influence on the container clarity. If, during reheating of the preform 115 (within the window of process stability), the temperature in the skin-layer (at the side of the core) is insufficiently high, the material undesirably may be ruptured apart during the stretch blow molding (stage two) process, resulting in a rough inner container 10 surface and containers 10 having low clarity. Additionally, it has been observed that a low amount of “pre-blowing” (intermediate shape of the stretched and pre-blown preform part, i.e. before the final pressure is applied) may contribute to a relatively rough inner container 10 surface (i.e. undesirable high haze) for the same reason. More specifically the primary pressure, flow of air and pre-blow time usually need to be sufficiently high to prevent that the material gets ruptured apart what gives the part an undesirable high haze.

Correlation of Processing Parameters

In the practice of the invention, it is important that several variables and factors be correlated to each other. Variables that are important in the practice of the invention include, for example, injection speed, MFI of the polypropylene-containing resin, the preform article thickness. In some instances, the gate diameter used during injection of the preform article is a factor. These factors may be optimized and correlated to each other for a given container application, as in the Critical Filling Rate Model set forth below. It is possible using the practice of the invention to maximize productivity of the preform and to maximize productivity polypropylene containers in a two-stage stretch blow molding process.

In one particularly useful aspect of the invention, a preform thickness may be of a value less than about 3.5 mm. Thickness is measured along side walls 101,104 as shown in FIG. 4A, measured as the maximum or thickest portion of the side wall. In yet another embodiment of the invention, the preform thickness may be in the range of about 2-3.5 mm. Furthermore, in the practice of the invention it has been found that an injection fill rate into the cavity mold of greater than about 5 grams of chemical composition (resin) per second is quite useful. Furthermore, in other aspects of the invention it is advantageous to use a cavity mold fill rate of between 5 and 22 grams per second.

Table A shows a correlation between processing variables in the practice of the invention. In Table A, the MFI values and preform wall thickness values are correlated to the optimized injection mold filling rate in the practice of the invention. It is important to note in Table A that for a given preform wall thickness an increase in the MFI value allows an operator to use a higher injection mold filling rate while still obtaining containers 10 of sufficient clarity. Thus, as a result of the practice of the invention it is possible to reduce the cycle time as compared to prior art processes, and yet still obtain containers of relatively low haze and high quality.

Looking from left to right in Table A, a greater preform wall thickness at a given level of MFI value enables an operator employing the invention to use an injection mold filling rate which is greater, resulting in faster production, reduced cycle times, and good container clarity.

Table A reports values for a (valve) gate thickness of 1.5 mm. In the practice of the invention, the use of a wider gate such as about 3.8 mm can result in a filling rate of about 13 g/sec at a MFI value of 13. This compares to the data in Table A in which a MFI of 13 at a (valve) gate diameter of 1.5 mm was successfully employed using an injection speed of about 5-6 g/sec. Furthermore, it has been found in the practice of the invention that using a (valve) gate diameter of 3.8 mm at MFI value 20 may result in an injection speed of about 22 g/sec. This value of 22 g/sec may be compared to the injection speed shown in Table A (valve diameter 1.5 mm) of 5-7 g/s.

TABLE A
Processing Variables Correlated to Injection
Mold Filling Rate for Invention*
	Preform Wall Thickness
	MFI		2 mm		3 mm	4 mm
	1.5	Poor	Poor	Poor
		Clarity	Clarity	Clarity
	13	4-5	g/s	4-5	g/s	5-6	g/s
	20	5	g/s	5-7	g/s	7-10	g/s
	30	6-7	g/s	10-13	g/s	13-17	g/s
	45	11	g/s	20	g/s	N/A
	*Values in Table A are provided for a (valve) gate diameter of 1.5 mm.

Measurements of percent haze/thickness ratios have been obtained on various containers 10 in the practice of the invention. It has been found that a percent haze/thickness reported as percent haze/mils with a value of less than about 0.05 is particularly highly desirable.

In the practice of the invention, it is possible in a manufacturing operation to achieve a rate of container production of greater than about 900 containers per hour per mold. In other applications, it is possible to provide a stretch blow molding step in a manufacturing operation at a rate of container production of at least about 1200 containers per hour per mold. In an even more desirable aspect, the invention makes it possible to achieve a rate of container production of at least about 1500 containers per hour per mold.

The following examples illustrate preferred specific details of the above described blow molding processes for producing clear, transparent, glossy containers (“bottles”) from polypropylene-containing preforms.

EXAMPLE 1

38 mm Neck, 4 mm Wall Preforms

Commercial random copolymer resins containing Millad 3988 (Borealis) were used to produce preforms as indicated in Table I. The preforms were produced on a two-cavity mold (only one cavity installed) 100 ton Netstal injection molding machine with a variable injection time (0.5-4.0 sec) and a constant cooling time of 22 sec. Melt temperature was 230° C. Temperature of the cooling water was 13° C. The holding pressure time was 9.2 sec. Total cycle time was around 37 sec (not optimized). A valve gate with a diameter of 1.5 mm was used. The preforms have a wall thickness of 4 mm and a bottle weight of about 25.3 g. These preforms were later blown into bottles as explained in subsequent examples.

TABLE I
Example 1 Preforms
			MFI	Injection	Injection
			(g/10	Time	Speed
	Example	Resin	sec)	(sec)	(g/sec)
	I-1	RB307MO	1.5	0.5	50.6
	I-2	RB307MO	1.5	1.0	25.3
	I-3	RB307MO	1.5	1.5	16.9
	I-4	RB307MO	1.5	2.0	12.7
	I-5	RB307MO	1.5	2.5	10.1
	I-6	RB307MO	1.5	3.0	8.4
	I-7	RB307MO	1.5	3.5	7.2
	I-8	RB307MO	1.5	4.0	6.3
	I-9	RE420MO	13	0.5	50.6
	I-10	RE420MO	13	1.0	25.3
	I-11	RE420MO	13	1.5	16.9
	I-12	RE420MO	13	2.0	12.7
	I-13	RE420MO	13	2.5	10.1
	I-14	RE420MO	13	3.0	8.4
	I-15	RE420MO	13	3.5	7.2
	I-16	RE420MO	13	4.0	6.3
	I-17	RF365MO	20	0.5	50.6
	I-18	RF365MO	20	1.0	25.3
	I-19	RF365MO	20	1.5	16.9
	I-20	RF365MO	20	2.0	12.7
	I-21	RF365MO	20	2.5	10.1
	I-22	RF365MO	20	3.0	8.4
	I-23	RF365MO	20	3.5	7.2
	I-24	RF365MO	20	4.0	6.3
	I-25	RG460MO	30	0.5	50.6
	I-26	RG460MO	30	1.0	25.3
	I-27	RG460MO	30	1.5	16.9
	I-28	RG460MO	30	2.0	12.7
	I-29	RG460MO	30	2.5	10.1
	I-30	RG460MO	30	3.0	8.4
	I-31	RG460MO	30	3.5	7.2
	I-32	RG460MO	30	4.0	6.3
	I-33	RJ370MO	45	0.5	50.6
	I-34	RJ370MO	45	1.0	25.3
	I-35	RJ370MO	45	1.5	16.9
	I-36	RJ370MO	45	2.0	12.7
	I-37	RJ370MO	45	2.5	10.1
	I-38	RJ370MO	45	3.0	8.4
	I-39	RJ370MO	45	3.5	7.2
	I-40	RJ370MO	45	4.0	6.3

EXAMPLE 2

38 mm Neck, 3 mm Wall Performs

Commercial random copolymer resins containing Millad 3988 (Borealis) were used to produce preforms as indicated in Table II. The preforms were produced on a two-cavity mold (only one cavity installed) 100 ton Netstal injection molding machine with a variable injection time (0.5-4.0 sec) and a constant cooling time of 10 sec. Melt temperature was 230° C. Temperature of the cooling water was 13° C. The holding pressure time was 4.5 sec. Total cycle time was around 20 sec (not optimized). A valve gate with a diameter of 1.5 mm was used. The preforms have a wall thickness of 3 mm and a bottle weight of about 20.3 g. These preforms were later blown into bottles as explained in subsequent examples.

TABLE II
Example 2 Preforms
			MFI	Injection	Injection
			(g/10	Time	Speed
	Example	Resin	sec)	(sec)	(g/sec)
	II-1	RB307MO	1.5	0.5	40.6
	II-2	RB307MO	1.5	1.0	20.3
	II-3	RB307MO	1.5	1.5	13.5
	II-4	RB307MO	1.5	2.0	10.2
	II-5	RB307MO	1.5	2.5	8.1
	II-6	RB307MO	1.5	3.0	6.8
	II-7	RB307MO	1.5	3.5	5.8
	II-8	RB307MO	1.5	4.0	5.1
	II-9	RE420MO	13	0.5	40.6
	II-10	RE420MO	13	1.0	20.3
	II-11	RE420MO	13	1.5	13.5
	II-12	RE420MO	13	2.0	10.2
	II-13	RE420MO	13	2.5	8.1
	II-14	RE420MO	13	3.0	6.8
	II-15	RE420MO	13	3.5	5.8
	II-16	RE420MO	13	4.0	5.1
	II-17	RF365MO	20	0.5	40.6
	II-18	RF365MO	20	1.0	20.3
	II-19	RF365MO	20	1.5	13.5
	II-20	RF365MO	20	2.0	10.2
	II-21	RF365MO	20	2.5	8.1
	II-22	RF365MO	20	3.0	6.8
	II-23	RF365MO	20	3.5	5.8
	II-24	RF365MO	20	4.0	5.1
	II-25	RG460MO	30	0.5	40.6
	II-26	RG460MO	30	1.0	20.3
	II-27	RG460MO	30	1.5	13.5
	II-28	RG460MO	30	2.0	10.2
	II-29	RG460MO	30	2.5	8.1
	II-30	RG460MO	30	3.0	6.8
	II-31	RG460MO	30	3.5	5.8
	II-32	RG460MO	30	4.0	5.1
	II-33	RJ370MO	45	0.5	40.6
	II-34	RJ370MO	45	1.0	20.3
	II-35	RJ370MO	45	1.5	13.5
	II-36	RJ370MO	45	2.0	10.2
	II-37	RJ370MO	45	2.5	8.1
	II-38	RJ370MO	45	3.0	6.8
	II-39	RJ370MO	45	3.5	5.8
	II-40	RJ370MO	45	4.0	5.1

EXAMPLE 3

38 mm Neck, 2 mm Wall Preforms

Commercial random copolymer resins containing Millad 3988 (Borealis) were used to produce preforms as indicated in Table ll. The preforms were produced on a two-cavity mold (only one cavity installed) 100 ton Netstal injection molding machine with a variable injection time (0.5-4.0 sec) and a constant cooling time of 10 sec. Melt temperature was 230° C. Temperature of the cooling water was 13° C. The holding pressure time was 2 sec. Total cycle time was around 20 sec (not optimized). A valve gate with a diameter of 1.5 mm was used. The preforms have a wall thickness of 2 mm and a bottle weight of about 17.3 g. These preforms were later blown into bottles as explained in subsequent examples.

TABLE III
Example 3 Preforms
			MFI	Injection	Injection
			(g/10	Time	Speed
	Example	Resin	sec)	(sec)	(g/sec)
	III-1	RB307MO	1.5	0.5	34.6
	III-2	RB307MO	1.5	1.0	17.3
	III-3	RB307MO	1.5	1.5	11.5
	III-4	RB307MO	1.5	2.0	10.2
	III-5	RB307MO	1.5	2.5	6.9
	III-6	RB307MO	1.5	3.0	5.8
	III-7	RB307MO	1.5	3.5	4.9
	III-8	RB307MO	1.5	4.0	4.3
	III-9	RE420MO	13	0.5	34.6
	III-10	RE420MO	13	1.0	17.3
	III-11	RE420MO	13	1.5	11.5
	III-12	RE420MO	13	2.0	10.2
	III-13	RE420MO	13	2.5	6.9
	III-14	RE420MO	13	3.0	5.8
	III-15	RE420MO	13	3.5	4.9
	III-16	RE420MO	13	4.0	4.3
	III-17	RF365MO	20	0.5	34.6
	III-18	RF365MO	20	1.0	17.3
	III-19	RF365MO	20	1.5	11.5
	III-20	RF365MO	20	2.0	10.2
	III-21	RF365MO	20	2.5	6.9
	III-22	RF365MO	20	3.0	5.8
	III-23	RF365MO	20	3.5	4.9
	III-24	RF365MO	20	4.0	4.3
	III-25	RG460MO	30	0.5	34.6
	III-26	RG460MO	30	1.0	17.3
	III-27	RG460MO	30	1.5	11.5
	III-28	RG460MO	30	2.0	10.2
	III-29	RG460MO	30	2.5	6.9
	III-30	RG460MO	30	3.0	5.8
	III-31	RG460MO	30	3.5	4.9
	III-32	RG460MO	30	4.0	4.3
	III-33	RJ370MO	45	0.5	34.6
	III-34	RJ370MO	45	1.0	17.3
	III-35	RJ370MO	45	1.5	11.5
	III-36	RJ370MO	45	2.0	10.2
	III-37	RJ370MO	45	2.5	6.9
	III-38	RJ370MO	45	3.0	5.8
	III-39	RJ370MO	45	3.5	4.9
	III-40	RJ370MO	45	4.0	4.3

EXAMPLE 4

38 mm Neck Bottles Produced Using Old ISBM Machine with 4 mm Performs

Polypropylene bottles (330 ml) were on a two-cavity Chia-Ming stretch blow molding machine designed to blow polypropylene bottles from preforms described in Example 1. Axial stretch ratio is 1.9/1, Hoop Stretch ratio=2.5/1 & Total Stretch Ratio=4.8/1. This machine is equipped with 3 heater boxes per cavity & uses 1000 Watt IR lamps. Pre-blow pressure was 6 bar & final pressure was 8 bar. After optimization, the bottle productivity for the preforms with 4 mm thickness was 820 bph/cav. Bottle quality was judged at the time of production to be Unacceptable (poorly blown bottle or blown out), Acceptable (a fully blown bottle with moderate optical properties), Average (a fully blown bottle with improved optical properties), or Excellent (a fully blown bottle with outstanding optical clarity).

TABLE IV
Example 4 Bottles
		MFI	Injection
		(g/10	Speed	% Haze/	Bottle
	Example	sec)	(g/sec)	thickness	Quality
	IV-1	1.5	50.6	1.252	Acceptable
	IV-2	1.5	25.3		Acceptable
	IV-3	1.5	16.9		Acceptable
	IV-4	1.5	12.7	1.530	Acceptable
	IV-5	1.5	10.1		Acceptable
	IV-6	1.5	8.4		Acceptable
	IV-7	1.5	7.2		Acceptable
	IV-8	1.5	6.3		Acceptable
	IV-9	13	50.6		Acceptable
	IV-10	13	25.3		Acceptable
	IV-11	13	16.9		Acceptable
	IV-12	13	12.7		Acceptable
	IV-13	13	10.1		Acceptable
	IV-14	13	8.4		Average
	IV-15	13	7.2	0.067	Excellent
	IV-16	13	6.3	0.043	Excellent
	IV-17	20	50.6		Acceptable
	IV-18	20	25.3		Acceptable
	IV-19	20	16.9		Acceptable
	IV-20	20	12.7		Average
	IV-21	20	10.1	0.782	Average
	IV-22	20	8.4		Excellent
	IV-23	20	7.2		Excellent
	IV-24	20	6.3	0.036	Excellent
	IV-25	30	50.6	1.191	Acceptable
	IV-26	30	25.3	0.150	Acceptable
	IV-27	30	16.9	0.062	Excellent
	IV-28	30	12.7		Excellent
	IV-29	30	10.1		Excellent
	IV-30	30	8.4		Excellent
	IV-31	30	7.2	0.075	Excellent
	IV-32	30	6.3		Excellent
	IV-33	45	50.6		NA
	IV-34	45	25.3		NA
	IV-35	45	16.9		NA
	IV-36	45	12.7		NA
	IV-37	45	10.1		NA
	IV-38	45	8.4		NA
	IV-39	45	7.2		NA
	IV-40	45	6.3	0.072	NA

EXAMPLE 5

38 mm Neck Bottles Produced Using Old ISBM Machine with 3 mm Preforms

Polypropylene bottles (330 ml) were blown at high speed on a two-cavity Chia-Ming stretch blow molding machine designed to blow polypropylene bottles from preforms described in Example 2. Axial stretch ratio is 1.9/1, Hoop Stretch ratio=2.4 & Total Stretch Ratio=4.6/1. This machine is equipped with 3 heater boxes per cavity & uses 1000 Watt IR lamps. Pre-blow pressure was 6 bar & final pressure was 8 bar. After optimization, the bottle productivity for the preforms with 3 mm thickness was 1,030 bph/cav. Bottle quality was judged at the time of production to be Unacceptable (poorly blown bottle or blown out), Acceptable (a fully blown bottle with moderate optical properties), Average (a fully blown bottle with improved optical properties), or Excellent (a fully blown bottle with outstanding optical clarity).

TABLE V
Example 5 Bottles
		MFI	Injection
		(g/10	Speed	% Haze/	Bottle
	Example	sec)	(g/sec)	thickness	Quality
	V-1	1.5	40.6		Acceptable
	V-2	1.5	20.3		Acceptable
	V-3	1.5	13.5		Acceptable
	V-4	1.5	10.2		Acceptable
	V-5	1.5	8.1		Acceptable
	V-6	1.5	6.8		Acceptable
	V-7	1.5	5.8		Acceptable
	V-8	1.5	5.1	2.143	Acceptable
	V-9	13	40.6		Acceptable
	V-10	13	20.3		Acceptable
	V-11	13	13.5		Acceptable
	V-12	13	10.2		Acceptable
	V-13	13	8.1		Acceptable
	V-14	13	6.8		Acceptable
	V-15	13	5.8		Average
	V-16	13	5.1		Excellent
	V-17	20	40.6		Acceptable
	V-18	20	20.3		Acceptable
	V-19	20	13.5		Acceptable
	V-20	20	10.2		Average
	V-21	20	8.1		Average
	V-22	20	6.8	0.132	Average
	V-23	20	5.8		Excellent
	V-24	20	5.1	0.056	Excellent
	V-25	30	40.6	0.125	Acceptable
	V-26	30	20.3		Acceptable
	V-27	30	13.5		Acceptable
	V-28	30	10.2		Excellent
	V-29	30	8.1		Excellent
	V-30	30	6.8		Excellent
	V-31	30	5.8	0.075	Excellent
	V-32	30	5.1		Excellent
	V-33	45	40.6		Acceptable
	V-34	45	20.3		Average
	V-35	45	13.5		Excellent
	V-36	45	10.2		Excellent
	V-37	45	8.1		Excellent
	V-38	45	6.8		Excellent
	V-39	45	5.8		Excellent
	V-40	45	5.1		Excellent

EXAMPLE 6

38 mm Neck Bottles Produced Using Old ISBM Machine with 2 mm Preforms

Polypropylene bottles (330 ml) were blown at high speed on a two-cavity Chia-Ming stretch blow molding machine designed to blow polypropylene bottles from preforms described in Example 3. Axial stretch ratio is 1.9/1, Hoop Stretch ratio=2.4 & Total Stretch Ratio=4.4/1. This machine is equipped with 3 heater boxes per cavity & uses 1000 Watt IR lamps. Pre-blow pressure was 6 bar & final pressure was 8 bar. After optimization, the bottle productivity for the preforms with 2 mm thickness was 1,200 bph/cav. Bottle quality was judged at the time of production to be Unacceptable (poorly blown bottle or blown out), Acceptable (a fully blown bottle with moderate optical properties), Average (a fully blown bottle with improved optical properties), or Excellent (a fully blown bottle with outstanding optical clarity).

TABLE VI
Example 6 Bottles
		MFI	Injection
		(g/10	Speed	% Haze/	Bottle
	Example	sec)	(g/sec)	thickness	Quality
	VI-1	1.5	34.6		Acceptable
	VI-2	1.5	17.3		Acceptable
	VI-3	1.5	11.5		Acceptable
	VI-4	1.5	10.2		Acceptable
	VI-5	1.5	6.9		Acceptable
	VI-6	1.5	5.8		Acceptable
	VI-7	1.5	4.9		Acceptable
	VI-8	1.5	4.3		Acceptable
	VI-9	13	34.6		Acceptable
	VI-10	13	17.3		Acceptable
	VI-11	13	11.5		Acceptable
	VI-12	13	10.2		Acceptable
	VI-13	13	6.9		Acceptable
	VI-14	13	5.8		Acceptable
	VI-15	13	4.9		Acceptable
	VI-16	13	4.3		Average
	VI-17	20	34.6		Acceptable
	VI-18	20	17.3		Acceptable
	VI-19	20	11.5		Acceptable
	VI-20	20	10.2		Acceptable
	VI-21	20	6.9		Acceptable
	VI-22	20	5.8		Average
	VI-23	20	4.9		Excellent
	VI-24	20	4.3		Excellent
	VI-25	30	34.6		Acceptable
	VI-26	30	17.3		Acceptable
	VI-27	30	11.5		Acceptable
	VI-28	30	10.2		Acceptable
	VI-29	30	6.9		Excellent
	VI-30	30	5.8		Excellent
	VI-31	30	4.9		Excellent
	VI-32	30	4.3		Excellent
	VI-33	45	34.6		Acceptable
	VI-34	45	17.3		Average
	VI-35	45	11.5		Excellent
	VI-36	45	10.2		Excellent
	VI-37	45	6.9		Excellent
	VI-38	45	5.8		Excellent
	VI-39	45	4.9		Excellent
	VI-40	45	4.3	0.087	Excellent

EXAMPLE 7

38 mm Neck Bottles Produced Using New ISBM Machine with 4 mm Preforms

Polypropylene bottles (500 ml) were blown at high speed (1500 bottles/cavity/hour) on a Sidel SBO-8 Series II stretch blow molding machine designed to blow PET preforms using the polypropylene preforms described in Example 1. Axial stretch ratio is 2.5/1, Hoop Stretch ratio=2.63 & Total Stretch Ratio=6.57/1.

Machine settings were adjusted to accommodate high clarity, high speed bottle production. Preforms were subjected to a pre-blow pressure of 3 Bar for 0.9 seconds with the preform inner temperature set to about 125°-130° C. and the outer temperature set to about 120°-125° C. Heating power distribution was managed in the range of 90%. Bottle quality was judged at the time of production to be Unacceptable (poorly blown bottle or blown out), Acceptable (a fully blown bottle with moderate optical properties), Average (a fully blown bottle with improved optical properties), or excellent (a fully blown bottle with outstanding optical clarity).

TABLE VII
Example 7 Bottles
		MFI	Injection
		(g/10	Speed	% Haze/	Bottle
	Example	sec)	(g/sec)	thickness	Quality
	VII-1	1.5	50.6		Acceptable
	VII-2	1.5	25.3		Acceptable
	VII-3	1.5	16.9		Acceptable
	VII-4	1.5	12.7		Acceptable
	VII-5	1.5	10.1		Acceptable
	VII-6	1.5	8.4		Acceptable
	VII-7	1.5	7.2		Acceptable
	VII-8	1.5	6.3	1.500	Acceptable
	VII-9	13	50.6		Acceptable
	VII-10	13	25.3		Acceptable
	VII-11	13	16.9	1.474	Acceptable
	VII-12	13	12.7	0.494	Acceptable
	VII-13	13	10.1	0.283	Average
	VII-14	13	8.4	0.205	Average
	VII-15	13	7.2	0.075	Excellent
	VII-16	13	6.3	0.089	Excellent
	VII-17	20	50.6		Acceptable
	VII-18	20	25.3	0.895	Acceptable
	VII-19	20	16.9	0.250	Acceptable
	VII-20	20	12.7	0.111	Acceptable
	VII-21	20	10.1	0.467	Acceptable
	VII-22	20	8.4	0.211	Average
	VII-23	20	7.2	0.086	Excellent
	VII-24	20	6.3	0.068	Excellent
	VII-25	30	50.6		Acceptable
	VII-26	30	25.3		Acceptable
	VII-27	30	16.9		Average
	VII-28	30	12.7	0.079	Excellent
	VII-29	30	10.1		Excellent
	VII-30	30	8.4		Excellent
	VII-31	30	7.2		Excellent
	VII-32	30	6.3	0.068	Excellent
	VII-33	45	50.6		Excellent
	VII-34	45	25.3		Excellent
	VII-35	45	16.9		Excellent
	VII-36	45	12.7		Excellent
	VII-37	45	10.1		Excellent
	VII-38	45	8.4		Excellent
	VII-39	45	7.2		Excellent
	VII-40	45	6.3		Excellent

EXAMPLE 8

38 mm Neck Bottles Produced Using New ISBM Machine with 3 mm Performs

Polypropylene bottles (500 ml) were blown at high speed (1,500 bottles/cavity/hour) on a Sidel SBO-8 Series-II stretch blow molding machine designed to blow PET preforms using the polypropylene preforms described in Example 2. Axial stretch ratio is 2.5/1, Hoop Stretch ratio=2.54 & Total Stretch Ratio=6.36/1. Machine settings were adjusted to accommodate high clarity, high speed bottle production. Preforms were subjected to a pre-blow pressure of 4.5 Bar for 0.4 seconds & nozzle for 3 rotations open activated at ‘point zero’. Blowing time is 0.8 sec & Exhaust time is 0.4 sec. Stretch speed is 1,384 m/sec & a standard stretch rod with 14 mm diameter was used. Preform temperature is about 120-130° C. Heating profile: Z1=75%,Z2=90%, Z3=70%, Z4=70%, Z5=65% & Z6=70% with Z1,Z5 & Z6 in an advanced position. % GP=65%. This example used 100% was ventilation to cool the preform surface. Total heating time, 14.65 sec, stabilization time=6.0 sec & final stabilization time=4.5 sec. Bottle quality was judged at the time of production to be Unacceptable (poorly blown bottle or blown out), Acceptable (a fully blown bottle with moderate optical properties), Average (a fully blown bottle with improved optical properties), or Excellent (a fully blown bottle with outstanding optical clarity).

TABLE VIII
Example 8 Bottles
		MFI	Injection
		(g/10	Speed	% Haze/	Bottle
	Example	sec)	(g/sec)	thickness	Quality
	VIII-1	1.5	40.6		Acceptable
	VIII-2	1.5	20.3		Acceptable
	VIII-3	1.5	13.5		Acceptable
	VIII-4	1.5	10.2		Acceptable
	VIII-5	1.5	8.1		Acceptable
	VIII-6	1.5	6.8		Acceptable
	VIII-7	1.5	5.8		Acceptable
	VIII-8	1.5	5.1	1.316	Acceptable
	VIII-9	13	40.6		Acceptable
	VIII-10	13	20.3		Acceptable
	VIII-11	13	13.5		Acceptable
	VIII-12	13	10.2		Acceptable
	VIII-13	13	8.1		Acceptable
	VIII-14	13	6.8		Acceptable
	VIII-15	13	5.8	0.087	Average
	VIII-16	13	5.1	0.074	Excellent
	VIII-17	20	40.6		Acceptable
	VIII-18	20	20.3		Acceptable
	VIII-19	20	13.5		Acceptable
	VIII-20	20	10.2	0.153	Average
	VIII-21	20	8.1		Average
	VIII-22	20	6.8		Excellent
	VIII-23	20	5.8		Excellent
	VIII-24	20	5.1	0.084	Excellent
	VIII-25	30	40.6		Acceptable
	VIII-26	30	20.3		Acceptable
	VIII-27	30	13.5	0.094	Average
	VIII-28	30	10.2		Excellent
	VIII-29	30	8.1		Excellent
	VIII-30	30	6.8		Excellent
	VIII-31	30	5.8		Excellent
	VIII-32	30	5.1	0.082	Excellent
	VIII-33	45	40.6		Acceptable
	VIII-34	45	20.3	0.192	Average
	VIII-35	45	13.5		Excellent
	VIII-36	45	10.2		Excellent
	VIII-37	45	8.1		Excellent
	VIII-38	45	6.8		Excellent
	VIII-39	45	5.8		Excellent
	VIII-40	45	5.1	0.072	Excellent

EXAMPLE 9

38 mm Neck Bottles Produced Using New ISBM Machine with 2 mm Preforms

Polypropylene bottles (500 ml) were blown at high speed (1,500 bottles/cavity/hour) on a Sidel SBO-8 Series-II stretch blow molding machine designed to blow PET preforms using the polypropylene preforms described in Example 3. Axial stretch ratio is 2.5/1, Hoop Stretch ratio=2.54 & Total Stretch Ratio=6.36/1. Machine settings were adjusted to accommodate high clarity, high speed bottle production. Preforms were subjected to a pre-blow pressure of 4 Bar for 0.4 seconds & nozzle for 3 rotations open activated at ‘point zero’. Blowing time is 0.8 sec & Exhaust time is 0.4 sec. Stretch speed is 1,384 m/sec & a standard stretch rod with 14 mm diameter was used. Preform temperature is about 115-127° C. Heating profile: Z1=72.5%,Z2=26%, Z3=26%, Z4=32.8%, Z5=26% & Z6=55.5% with Z1,Z5 & Z6 in an advanced position. % GP=45%. Used 100% ventilation to cool the preform surface. Total heating time is 14.65 sec, stabilization time=6.0 sec & final stabilization time=4.5 sec. Bottle quality was judged at the time of production to be Unacceptable (poorly blown bottle or blown out), Acceptable (a fully blown bottle with moderate optical properties), Average (a fully blown bottle with improved optical properties), or Excellent (a fully blown bottle with outstanding optical clarity).

TABLE IX
Example 9 Bottles
		MFI	Injection
		(g/10	Speed	% Haze/	Bottle
	Example	sec)	(g/sec)	thickness	Quality
	IX-1	1.5	34.6	3.462	Acceptable
	IX-2	1.5	17.3	2.722	Acceptable
	IX-3	1.5	11.5	2.300	Acceptable
	IX-4	1.5	10.2	2.053	Acceptable
	IX-5	1.5	6.9	2.250	Acceptable
	IX-6	1.5	5.8	2.000	Acceptable
	IX-7	1.5	4.9	2.000	Acceptable
	IX-8	1.5	4.3	1.824	Acceptable
	IX-9	13	34.6	2.537	Acceptable
	IX-10	13	17.3	1.739	Acceptable
	IX-11	13	11.5	1.833	Acceptable
	IX-12	13	10.2	0.545	Acceptable
	IX-13	13	6.9	0.154	Acceptable
	IX-14	13	5.8	0.146	Acceptable
	IX-15	13	4.9	0.160	Acceptable
	IX-16	13	4.3	0.115	Average
	IX-17	20	34.6	2.591	Acceptable
	IX-18	20	17.3	1.250	Acceptable
	IX-19	20	11.5	2.000	Acceptable
	IX-20	20	10.2	1.077	Acceptable
	IX-21	20	6.9	0.200	Acceptable
	IX-22	20	5.8	0.107	Average
	IX-23	20	4.9	0.186	Average
	IX-24	20	4.3		Excellent
	IX-25	30	34.6		Acceptable
	IX-26	30	17.3		Acceptable
	IX-27	30	11.5		Acceptable
	IX-28	30	10.2		Average
	IX-29	30	6.9	0.143	Average
	IX-30	30	5.8		Excellent
	IX-31	30	4.9		Excellent
	IX-32	30	4.3	0.100	Excellent
	IX-33	45	34.6	1.000	Acceptable
	IX-34	45	17.3	0.387	Acceptable
	IX-35	45	11.5	0.143	Average
	IX-36	45	10.2		Excellent
	IX-37	45	6.9		Excellent
	IX-38	45	5.8		Excellent
	IX-39	45	4.9		Excellent
	IX-40	45	4.3	0.092	Excellent

EXAMPLE 10

38 mm Neck, 3 mm Wall Preforms

Several compounds were produced on a Killion single screw extruder at a temperature 230° C. using 25 g/10 min random copolymer polypropylene fluff. The preforms (ref. Table X) were produced on a two-cavity mold (only one cavity installed) 100 ton Netstal injection molding machine with a variable injection time (0.5-4.0 sec) and a constant cooling time of 10 sec. Melt temperature was 230° C. Temperature of the cooling water was 13° C. The holding pressure time was 4.5 sec. Total cycle time was around 20 sec (not optimized). A valve gate with a diameter of 1.5 mm was used. The preforms have a wall thickness of 3 mm and a bottle weight of about 20.3 g. These preforms were later blown into bottles as explained in subsequent examples.

TABLE X
Example 10 Preforms
				Injection	Injection
			Loading	Time	Speed
	Example	Nucleator	(ppm)	(sec)	(g/sec)
	X-1	NA-21	2000	0.5	50.6
	X-2	NA-21	2000	1.0	25.3
	X-3	NA-21	2000	1.5	16.9
	X-4	NA-21	2000	2.0	12.7
	X-5	NA-21	2000	2.5	10.1
	X-6	NA-21	2000	3.0	8.4
	X-7	NA-21	2000	3.5	7.2
	X-8	NA-21	2000	4.0	6.3
	X-9	NA-11	1000	0.5	50.6
	X-10	NA-11	1000	1.0	25.3
	X-11	NA-11	1000	1.5	16.9
	X-12	NA-11	1000	2.0	12.7
	X-13	NA-11	1000	2.5	10.1
	X-14	NA-11	1000	3.0	8.4
	X-15	NA-11	1000	3.5	7.2
	X-16	NA-11	1000	4.0	6.3
	X-17	HPN-68	1000	0.5	50.6
	X-18	HPN-68	1000	1.0	25.3
	X-19	HPN-68	1000	1.5	16.9
	X-20	HPN-68	1000	2.0	12.7
	X-21	HPN-68	1000	2.5	10.1
	X-22	HPN-68	1000	3.0	8.4
	X-23	HPN-68	1000	3.5	7.2
	X-24	HPN-68	1000	4.0	6.3
	X-25	AlptBBA	1000	0.5	50.6
	X-26	AlptBBA	1000	1.0	25.3
	X-27	AlptBBA	1000	1.5	16.9
	X-28	AlptBBA	1000	2.0	12.7
	X-29	AlptBBA	1000	2.5	10.1
	X-30	AlptBBA	1000	3.0	8.4
	X-31	AlptBBA	1000	3.5	7.2
	X-32	AlptBBA	1000	4.0	6.3
	X-33	CaHHPA	1500	0.5	50.6
	X-34	CaHHPA	1500	1.0	25.3
	X-35	CaHHPA	1500	1.5	16.9
	X-36	CaHHPA	1500	2.0	12.7
	X-37	CaHHPA	1500	2.5	10.1
	X-38	CaHHPA	1500	3.0	8.4
	X-39	CaHHPA	1500	3.5	7.2
	X-40	CaHHPA	1500	4.0	6.3
	X-41	M3905	2000	0.5	50.6
	X-42	M3905	2000	1.0	25.3
	X-43	M3905	2000	1.5	16.9
	X-44	M3905	2000	2.0	12.7
	X-45	M3905	2000	2.5	10.1
	X-46	M3905	2000	3.0	8.4
	X-47	M3905	2000	3.5	7.2
	X-48	M3905	2000	4.0	6.3
	X-49	M3988	2000	0.5	50.6
	X-50	M3988	2000	1.0	25.3
	X-51	M3988	2000	1.5	16.9
	X-52	M3988	2000	2.0	12.7
	X-53	M3988	2000	2.5	10.1
	X-54	M3988	2000	3.0	8.4
	X-55	M3988	2000	3.5	7.2
	X-56	M3988	2000	4.0	6.3
	X-57	—	—	0.5	50.6
	X-58	—	—	1.0	25.3
	X-59	—	—	1.5	16.9
	X-60	—	—	2.0	12.7
	X-61	—	—	2.5	10.1
	X-62	—	—	3.0	8.4
	X-63	—	—	3.5	7.2
	X-64	—	—	4.0	6.3

EXAMPLE 11

38 mm Neck Bottles Produced Using Old ISBM Machine With 3 mm Preforms

Polypropylene bottles (330 ml, ref. Table XI) were produced blown at high speed on a two-cavity Chia-Ming stretch blow molding machine designed to blow polypropylene bottles from preforms described in Example 10. Axial stretch ratio is 1.9/1, Hoop Stretch ratio=2.4 & Total Stretch Ratio=4.6/1. This machine is equipped with 3 heater boxes per cavity & uses 1000 Watt IR lamps. Pre-blow pressure was 6 bar & final pressure was 8 bar. After optimization, the bottle productivity for the preforms with 3 mm thickness was 1,030 bph/cav. Bottle quality was judged at the time of production to be Unacceptable (poorly blown bottle or blown out), Acceptable (a fully blown bottle with moderate optical properties), Average (a fully blown bottle with improved optical properties), or Excellent (a fully blown bottle with outstanding optical clarity).

TABLE XI
Example 11 Bottles
			Injection
		Loading	Speed	% Haze/	Bottle
Example	Nucleator	(ppm)	(g/sec)	thickness	Quality
XI-1	NA-21	2000	50.6	2.048	Acceptable
XI-2	NA-21	2000	25.3	1.500	Average
XI-3	NA-21	2000	16.9	0.130	Excellent
XI-4	NA-21	2000	12.7	0.079	Excellent
XI-5	NA-21	2000	10.1	0.074	Excellent
XI-6	NA-21	2000	8.4	0.076	Excellent
XI-7	NA-21	2000	7.2	0.100	Excellent
XI-8	NA-21	2000	6.3	0.052	Excellent
XI-9	NA-11	1000	50.6	2.000	Acceptable
XI-10	NA-11	1000	25.3	0.739	Average
XI-11	NA-11	1000	16.9	0.132	Excellent
XI-12	NA-11	1000	12.7	0.100	Excellent
XI-13	NA-11	1000	10.1	0.111	Excellent
XI-14	NA-11	1000	8.4	0.087	Excellent
XI-15	NA-11	1000	7.2	0.096	Excellent
XI-16	NA-11	1000	6.3	0.086	Excellent
XI-17	HPN-68	1000	50.6		Acceptable
XI-18	HPN-68	1000	25.3	1.565	Average
XI-19	HPN-68	1000	16.9		Excellent
XI-20	HPN-68	1000	12.7		Excellent
XI-21	HPN-68	1000	10.1		Excellent
XI-22	HPN-68	1000	8.4		Excellent
XI-23	HPN-68	1000	7.2		Excellent
XI-24	HPN-68	1000	6.3	0.121	Excellent
XI-25	AlptBBA	1000	50.6		Acceptable
XI-26	AlptBBA	1000	25.3	0.304	Average
XI-27	AlptBBA	1000	16.9		Excellent
XI-28	AlptBBA	1000	12.7		Excellent
XI-29	AlptBBA	1000	10.1		Excellent
XI-30	AlptBBA	1000	8.4		Excellent
XI-31	AlptBBA	1000	7.2		Excellent
XI-32	AlptBBA	1000	6.3	0.186	Excellent
XI-33	CaHHPA	1500	50.6		Acceptable
XI-34	CaHHPA	1500	25.3	0.880	Average
XI-35	CaHHPA	1500	16.9		Excellent
XI-36	CaHHPA	1500	12.7		Excellent
XI-37	CaHHPA	1500	10.1		Excellent
XI-38	CaHHPA	1500	8.4		Excellent
XI-39	CaHHPA	1500	7.2		Excellent
XI-40	CaHHPA	1500	6.3	0.100	Excellent
XI-41	M3905	2000	50.6		Acceptable
XI-42	M3905	2000	25.3	0.240	Average
XI-43	M3905	2000	16.9		Average
XI-44	M3905	2000	12.7		Excellent
XI-45	M3905	2000	10.1		Excellent
XI-46	M3905	2000	8.4		Excellent
XI-47	M3905	2000	7.2		Excellent
XI-48	M3905	2000	6.3	0.067	Excellent
XI-49	M3988	2000	50.6		Acceptable
XI-50	M3988	2000	25.3	1.826	Average
XI-51	M3988	2000	16.9		Average
XI-52	M3988	2000	12.7		Excellent
XI-53	M3988	2000	10.1		Excellent
XI-54	M3988	2000	8.4		Excellent
XI-55	M3988	2000	7.2		Excellent
XI-56	M3988	2000	6.3	0.058	Excellent
XI-57	—	—	50.6		Acceptable
XI-58	—	—	25.3	1.917	Average
XI-59	—	—	16.9		Excellent
XI-60	—	—	12.7		Excellent
XI-61	—	—	10.1		Excellent
XI-62	—	—	8.4		Excellent
XI-63	—	—	7.2		Excellent
XI-64	—	—	6.3	0.083	Excellent

EXAMPLE 12

38 mm Neck Bottles Produced Using New ISBM Machine with 3 mm Preforms

Polypropylene bottles (500 ml, table XII) were produced at high speed (1,500 bottles/cavity/hour) on a Sidel SBO-8 Series-II stretch blow molding machine designed to blow PET preforms using the polypropylene preforms described in Example 10. Axial stretch ratio is 2.5/1, Hoop Stretch ratio=2.54 & Total Stretch Ratio=6.36/1. Machine settings were adjusted to accommodate high clarity, high speed bottle production. Preforms were subjected to a pre-blow pressure of 4.5 Bar for 0.4 seconds & nozzle for 3 rotations open activated at ‘point zero’. Blowing time is 0.8 sec & Exhaust time is 0.4 sec. Stretch speed is 1,384 m/sec & a standard stretch rod with 14 mm diameter was used. Preform temperature is about 120-130° C. Heating profile: Z1=75%,Z2=90%, Z3=70%, Z4=70%, Z5=65% & Z6=70% with Z1,Z5 & Z6 in an advanced position. % GP=65%. The invention employed 100% ventilation to cool the preform surface. Total heating time is 14.65 sec, stabilization time=6.0 sec & final stabilization time=4.5 sec. Bottle quality was judged at the time of production to be Unacceptable (poorly blown bottle or blown out), Acceptable (a fully blown bottle with moderate optical properties), Average (a fully blown bottle with improved optical properties), or Excellent (a fully blown bottle with outstanding optical clarity).

TABLE XII
Example 12 Bottles
			Injection						Injection
		Loading	Speed	% Haze/	Bottle			Loading	Speed	% Haze/
Example	Nucleator	(ppm)	(g/sec)	thickness	Quality	Example	Nucleator	(ppm)	(g/sec)	thickness
XII-1	NA-21	2000	50.6		Acceptable	XII-33	CaHHPA	1500	50.6
XII-2	NA-21	2000	25.3		Average	XII-34	CaHHPA	1500	25.3
XII-3	NA-21	2000	16.9		Excellent	XII-35	CaHHPA	1500	16.9
XII-4	NA-21	2000	12.7		Excellent	XII-36	CaHHPA	1500	12.7
XII-5	NA-21	2000	10.1		Excellent	XII-37	CaHHPA	1500	10.1
XII-6	NA-21	2000	8.4		Excellent	XII-38	CaHHPA	1500	8.4
XII-7	NA-21	2000	7.2		Excellent	XII-39	CaHHPA	1500	7.2
XII-8	NA-21	2000	6.3	0.088	Excellent	XII-40	CaHHPA	1500	6.3	0.100
XII-9	NA-11	1000	50.6		Acceptable	XII-41	M3905	2000	50.6
XII-10	NA-11	1000	25.3		Average	XII-42	M3905	2000	25.3
XII-11	NA-11	1000	16.9		Excellent	XII-43	M3905	2000	16.9
XII-12	NA-11	1000	12.7		Excellent	XII-44	M3905	2000	12.7
XII-13	NA-11	1000	10.1		Excellent	XII-45	M3905	2000	10.1
XII-14	NA-11	1000	8.4		Excellent	XII-46	M3905	2000	8.4
XII-15	NA-11	1000	7.2		Excellent	XII-47	M3905	2000	7.2
XII-16	NA-11	1000	6.3	0.115	Excellent	XII-48	M3905	2000	6.3	0.048
XII-17	HPN-68	1000	50.6		Acceptable	XII-49	M3988	2000	50.6
XII-18	HPN-68	1000	25.3		Average	XII-50	M3988	2000	25.3
XII-19	HPN-68	1000	16.9		Excellent	XII-51	M3988	2000	16.9
XII-20	HPN-68	1000	12.7		Excellent	XII-52	M3988	2000	12.7
XII-21	HPN-68	1000	10.1		Excellent	XII-53	M3988	2000	10.1
XII-22	HPN-68	1000	8.4		Excellent	XII-54	M3988	2000	8.4
XII-23	HPN-68	1000	7.2		Excellent	XII-55	M3988	2000	7.2
XII-24	HPN-68	1000	6.3	0.116	Excellent	XII-56	M3988	2000	6.3	0.076
XII-25	AlptBBA	1000	50.6		Acceptable	XII-57	—	—	50.6
XII-26	AlptBBA	1000	25.3		Average	XII-58	—	—	25.3
XII-27	AlptBBA	1000	16.9		Excellent	XII-59	—	—	16.9
XII-28	AlptBBA	1000	12.7		Excellent	XII-60	—	—	12.7
XII-29	AlptBBA	1000	10.1		Excellent	XII-61	—	—	10.1
XII-30	AlptBBA	1000	8.4		Excellent	XII-62	—	—	8.4
XII-31	AlptBBA	1000	7.2		Excellent	XII-63	—	—	7.2
XII-32	AlptBBA	1000	6.3	0.164	Excellent	XII-64	—	—	6.3	0.062

EXAMPLE 13

28 mm Neck, 3 mm Wall Preforms

A commercial homopolymer resin containing Millad 3988 (Mosten MT 230 from Chemopetrol, MFI=30) & random copolymer (Borealis RF365 MO, MFI=20) was used to produce preforms as indicated in Table XIII. The preforms were produced on a two-cavity mold (only one cavity installed) 100 ton Netstal injection molding machine with a variable injection time (0.5-4.0 sec) and a constant cooling time of 10 sec. Melt temperature was 240° C. Temperature of the cooling water was 13° C. The holding pressure time was 8.4 sec. Total cycle time was around 25 sec (not optimized). A valve gate with a diameter of 1.5 mm was used. The preforms have a wall thickness of 3 mm and a bottle weight of about 20.3 g. These preforms were later blown into bottles as explained in subsequent examples.

TABLE XIII
Example 13 Preforms
			MFI	Injection	Injection
			(g/10	Time	Speed
	Example	Resin	sec)	(sec)	(g/sec)
	XIII-1	HP	30	0.5	50.6
		MT 230
	XIII-2	HP	30	1.0	25.3
		MT 230
	XIII-3	HP	30	1.5	16.9
		MT 230
	XIII-4	HP	30	2.0	12.7
		MT 230
	XIII-5	HP	30	2.5	10.1
		MT 230
	XIII-6	HP	30	3.0	8.4
		MT 230
	XIII-7	HP	30	3.5	7.2
		MT 230
	XIII-8	HP	30	4.0	6.3
		MT 230
	XIII-9	RF 365MO	20	2.5	50.6
	XIII-10	RF 365MO	20	3.0	25.3
	XIII-11	RF 365MO	20	3.5	16.9
	XIII-12	RF 365MO	20	4.0	12.7
	XIII-13	RF 365MO	20	0.5	10.1
	XIII-14	RF 365MO	20	1.0	8.4
	XIII-15	RF 365MO	20	1.5	7.2
	XIII-16	RF 365MO	20	2.0	6.3

EXAMPLE 14

28 mm Neck Bottles Produced Using New ISBM Machine With 3 mm Preforms

Polypropylene bottles (500 ml) having a narrow neck were produced at high speed (1500 bottles/cavity/hour) on a Sidel SBO-8 Series-II stretch blow molding machine designed to blow PET preforms using the polypropylene preforms described in Example 13. The following stretch ratios were used: axial stretch ratio of 2.63/1, radial stretch ratio of 3.08 and a total stretch ratio of 8.10/1. Machine settings were adjusted to accommodate high clarity, high speed bottle production. In case of the Chemopetrol MT230 resin (homopolymer with a MFI of about 30 g/10 min) the temperature measured at the outer side of the preform was 143.5° C. and 152.5° C. at the inner side of the preform. In case of the Borealis RF 365 MO (random copolymer with a MFI of 20 g/10 min) the temperature measured at the outer side of the preform was 127.5° C. and 134.8° C. at the inner side of the preform. Bottle quality was judged at the time of production to be Unacceptable (poorly blown bottle or blown out), Acceptable (a fully blown bottle with moderate optical properties), Average (a fully blown bottle with improved optical properties), or Excellent (a fully blown bottle with outstanding optical clarity).

TABLE XIV
Example 14 Bottles
			Injection
	MFI		Speed
	(g/10		(g/cc	% Haze/	Bottle
Example	sec)	Resin	sec)	thickness	Quality
XIV-1	30	MT230	50.6	2.427	Acceptable
		(HP)
XIV-2	30	MT230	25.3		Acceptable
		(HP)
XIV-3	30	MT230	16.9	0.583	Acceptable
		(HP)
XIV-4	30	MT230	12.7	0.373	Average
		(HP)
XIV-5	30	MT230	10.1	0.256	Excellent
		(HP)
XIV-6	30	MT230	8.4	0.274	Excellent
		(HP)
XIV-7	30	MT230	7.2	0.265	Excellent
		(HP)
XIV-8	30	MT230	6.3	0.163	Excellent
		(HP)
XIV-9	20	RF	50.6	50.6	Acceptable
		365MO
XIV-10	20	RF	25.3	25.3	Acceptable
		365MO
XIV-11	20	RF	16.9	16.9	Acceptable
		365MO
XIV-12	20	RF	12.7	12.7	Acceptable
		365MO
XIV-13	20	RF	10.1	10.1	Acceptable
		365MO
XIV-14	20	RF	8.4	8.4	Acceptable
		365MO
XIV-15	20	RF	7.2	7.2	Average
		365MO
XIV-16	20	RF	6.3	6.3	Excellent
		365MO

Thickness

For purposes of this specification, the thickness of preforms is measured along the side walls 101, 104 as shown in FIG. 4A, measured at the widest portion of the side walls 101,104.

Thickness of containers (bottles), such as for purposes of percent haze/thickness ratios is measured at the point at which the haze has been measured (see below), using a Magna-Mike 8500 Hall effect thickness gauge.

Haze

For purposes of this specification, haze has been measured on a BYK-Gardner hazemeter by ASTM Standard Test Method D1003-61 modified by use of an 0.2″ aperture. The area in which haze could be measured reliably was in relatively small areas less than about 0.5″ in area. Samples were obtained from sample containers (bottles) at a relatively flat point approximately mid-way to the bottom of the bottle after the transition point. A thickness modified haze was calculated for each sample where (H/t) is defined as the haze divided by the thickness at the point where the haze was measured.

Roughness on the inner container 10 surface has a negative influence on the container clarity. If, during reheating of the preform 115 (within the window of process stability), the temperature in the skin-layer is insufficiently high, the material undesirably may be ruptured apart during the stretch blow molding (stage two) process, resulting in a rough inner container 10 surface and containers 10 having low clarity.

Critical Filling Rate Model

In addition, experimentation was done to understand the relationships among the Melt Flow Index (MFI), the perform thickness, and the critical filling rate in two-stage injection stretch blow molded (ISBM) polypropylene articles.

The experimental data are given in Table XV. The preform thickness (T) is provided in units of millimeters, and the critical filling rate is in units of grams/second. The critical filling rate (sometimes called “FillingRate” herein) is believed to be the maximum filling rate (grams/second) for which acceptably clear articles are formed under the given conditions. A 1.5 millimeter valve gate was used for these experiments. Other valve gates values could be used to make similar models for such other valve gate sizes.

A mathematical regression fitted model was obtained for the critical filling rate using the data in Table XV. The model obtained for the critical filling rate is {Critical FillingRate}=14.14419−0.86045×{MFI}−3.28054×{Thickness}+0.24136×{MFI}×{Thickness}+0.01044×{MFI}×{MFI} wherein the square of the correlation coefficient for the model is R²=0.98 and the Root Mean Square Error for the model is RMSE=0.805. Each coefficient is statistically significant at a probability of 0.0079 or less, and the model as a whole is statistically significant at a probability of less than 0.0001. An interpretation of R² is that about 100×R²=98% of the variation observed among the FillingRate values is accounted for by the mathematical model. In short, the above mathematical model has been observed to be effective in describing essentially all the variation observed in the critical filling rate in terms of MFI and preform thickness.

The model describes or shows the boundary between unclear and acceptably clear injection molded articles. Thus, at a given melt flow index {MFI} value and {Thickness} value, acceptably clear molded articles are obtained at filling rates less than the critical filling rate {FillingRate} given by the above model. However, unclear molded articles are obtained at filling rates greater than the critical filling rate {FillingRate} given by the above model.

Plots of the data obtained which was used to prepare the experimental model are given in FIGS. 9-11.

FIG. 9 illustrates the model using a perspective view of the critical filling rate surface in terms of MFI and Thickness. FIG. 10 represents contours of constant FillingRate (critical filling rate) on this surface; and FIG. 11 represents the intersection of the critical filling rate surface with planes of constant thickness (Thickness=2, 3, and 4 millimeters).

FIG. 10 illustrates the model through a contour plot. The curves plotted are curves of constant Critical FillingRate as given by the model. For example, for the Critical FillingRate=10 grams/second contour, the MFI and Thickness values corresponding to points on this contour provide distinct ways to achieve the critical filling rate of 10 grams/second.

FIG. 11 illustrates the model through how the surface intersects selected planes perpendicular to the plane of the MFI and Thickness axes of FIG. 9. The intersections of the three planes of constant Thickness=2, 3, and 4 millimeters with the model surface are plotted in FIG. 11. In addition, the experimental data points of Table XV are also plotted. Note that there are two sets of MFI and Thickness data having the same values so that two of the plotted positions represent two experimental values each.

Attached are results from testing performed with respect to determining the effect of the injection valve gate diameter and fill rate on the haze of ISBM PP bottles.

TABLE XV
Melt Flow Index, Preform Thickness, and Injection Rate Factors
Employed to Construct Model of Critical Filling Rate (data
obtained using a 1.5 mm valve gate diameter)
	Obs	MFI	Thickness	Rate
	1	13	2	4
	2	13	3	4
	3	13	4	5
	4	20	2	5
	5	20	3	5
	6	20	4	7
	7	30	2	6
	8	30	3	10
	9	30	4	13
	10	45	2	11
	11	45	3	20

EXAMPLE 15

Fill Rates and Gate Diameter

Preforms were made with FillRates ranging from 5.5 to 40.2 grams per second utilizing two different resins—Borealis RF365MO (20 MI RCP) and Atofina 7525 (12 MI RCP). Three different injection valve gates were utilized in the preform production—1.5, 3.0, and 3.8 mm. Four different conditions were used to produce the SBM bottles—The bottles were produced with a % Production Power of 83% (Oven Temperature=79° C.) and Preblow=0.7 seconds. Haze was measured in the middle of the bottle on the third rib of the bottle from the top using a BYK Gardner hazemeter as described in Example 14. In general, it has been found that haze is dependent upon FillRate. There is a strong increase in haze in both of the resins with increasing FillRate. The Borealis resin reaches a minimum % haze at a faster fill rate than does the Atofina resin, indicating an interaction and influence of the MI of the resin with fill rate.

There is an effect of the valve gate diameter as it can be seen that the change in haze of both of the resins (see attached Table XVI). A 3.8 mm valve gate shows a different dependency of % haze on fill time than do the 1.5 and 3.0 mm gates.

TABLE XVI
Fill Rate Conditions and Results
		Gate	Fill
Fill	Resin	Diameter	Rate		Thickness	Haze/
Rate	MI	(mm)	(g/sec)	Haze	(mil)	Thickness
	20	1.5	40.2	42.1	17.6	2.39
			27.7	20.6	15.5	1.33
			20.3	21.8	14.2	1.54
			17.3	7.49	13.9	0.54
			13.9	3.71	14.6	0.25
			12	2.57	14.6	0.18
			10.5	2.45	14.7	0.17
			9.2	1.48	14.8	0.10
			8.5	1.98	15.4	0.13
			5.7	1.85	14.9	0.12
	20	3.0	38	46	14	3.29
			27.7	46.3	15.8	2.93
			20.1	14.1	15.1	0.93
			16.9	5.49	16.7	0.33
			14.2	3.56	13.5	0.26
			12.2	1.71	13.5	0.13
			10.8	1.7	14.6	0.12
			9.5	0.99	14.8	0.07
			8.7	1.3	14	0.09
			5.5	2.04	13.6	0.15
	20	3.8	38	35.9	15.7	2.29
			27	7.04	16.5	0.43
			20.1	5.98	14.3	0.42
			16.9	3.15	15.1	0.21
			14.2	2.09	15.1	0.14
			12.1	2.27	13.5	0.17
			10.8	1.58	13.2	0.12
			9.5	1.36	14.5	0.09
			8.3	1.53	13.4	0.11
			5.5	1.7	13.8	0.12
	10	1.5	38.7	41	17.6	2.33
			30.4	44	15.9	2.77
			20.3	39	15.5	2.52
			16.9	31.1	15.2	2.05
			13.9	18.3	14	1.31
			11.9	18.6	13.4	1.39
			10.6	14.4	13.9	1.04
			9.2	4.53	16.6	0.27
			8.6	3.76	13.6	0.28
			5.7	2.5	14.2	0.18
			37.4
			28
			20.1
			16.9
			14.2
			12.2
			10.8
			9.5
			8.3
			5.5
			37.4	51	16.3	3.13
			28	39.2	16.9	2.32
			20.1	20.8	15.6	1.33
			16.9	29.4	13.2	2.23
			14.2	22	14.7	1.50
			12.2	6.22	15.3	0.41
			10.8	4.5	14.4	0.31
			9.5	3.85	12.5	0.31
			8.3	2.3	15.7	0.15
			5.5	1.99	12.9	0.15

The data of Table XVI were used to calculate a critical fill rate (FillRate) as described above in “Critical Fill Rate Model”. The data for each MFI and gate diameter were plotted. The filling rate corresponding to a normalized haze unit of 0.2 was estimated from the plots. This value of filling rate was taken as the critical filling rate (FillingRate). The critical filling rates obtained by this method are given in Table XVII. The critical filling rate describes the boundary between unclear and acceptably clear injection molded articles in terms of normalized haze. At a given MFI value and gate diameter, acceptably clear molded articles are obtained at filling rates less than the critical filling rate (FillingRate). Unclear parts are obtained at filling rates greater than the critical filling rate (FillingRate).

Table XVII shows that there is a strong interaction between gate diameter and the MFI of the resin in order to manufacture a bottle having acceptable haze, as demonstrated by the variation in the FillingRate as a function of gate diameter and MFI.

TABLE XVII
Gate Diameter (mm)	MFI	FillingRate (g/sec)
1.5	10	7
1.5	20	12
3.8	10	9
3.8	20	16

Furthermore, for a gate diameter of about 3.0, it is believed that a filling rate of about 14 g/sec could be employed, at an MFI of about 20.

EXAMPLE 16

Effect of the Pre-Blow Conditions Upon Bottle Clarity

The effect of pre-blow pressure and pre-blow time on bottle transparency is demonstrated in the example 16. A 15.5 gram preform (wall thickness is 3 mm) made from Borealis RF 365 MO random copolymer polypropylene resin (having a MI=20) was injected on an Engel injection machine equipped with a two-cavity Hofstetter preform mold (1.5 mm valve gate) with a melt temperature of 230° C., fill time of 4 seconds and a total cycle-time of 20 seconds. The preforms were blown into bottles on a Sidel SBO-6 machine Series-II machine equipped with a linear oven at the maximal productivity of 1,400 bottles per hour and cavity. The bottles are round in shape, have a capacity of 250 ml, a neck diameter of 40 mm and the stretch ratio's are: axial stretch ratio=2.5/1; hoop-stretch ratio=2.53/1 & total stretch ratio=6.25/1. The following processing conditions were used to produce the bottles: production power=85%; ventilation=80%; overall power for the individual heating zones Z1=92.5%; Z2=85%; Z3=11.3%; Z4=69.8% & Z5=79.8%. Final blowing pressure=17 bar. The following pre-blow conditions gave the best results: pre-blow pressure=3 bar; pre-blow time=0.2 sec; pre-blow delay=point ‘0’; flow of air=valve is 3 revolutions open. With these processing conditions (i.e. our ‘reference’ process) we obtained high clarity polypropylene bottles. By changing one variable at a time, we determined the high and low values allowing us to produce high quality clear polypropylene bottles.

	Pre-blow pressure:	1	bar (very hazy in panel)
		2	bar (slightly hazy in panel)
		3	bar (clear)
		4	bar (clear)
		5	bar (clear)
		7	bar (clear)
		10	bar (clear).
	Pre-blow time:	0	sec (very hazy in panel)
		0.05	sec (slightly hazy in panel)
		0.1	sec (slightly hazy)
		0.2	sec (clear)
		0.4	sec (clear)
		0.8	sec (clear)

Pre-blow pressure and pre-blow time do have a very significant effect on the bottle clarity. A minimal pre-blow pressure (2 bar) and pre-blow time (0.2 sec) respectively are required to obtain bottles with excellent optical properties. Below these critical values of pre-blow pressure and pre-blow time, it may not be possible to achieve high clarity bottles. In other words, it is possible to produce bottles with better clarity if the pre-blow (which is an intermediate state between preform & finished bottle) is more developed. The development of a pre-blow can be best described by filling it up with water, weighing it and expressing it as a percentage of a filled finished bottle. Our conclusion is that polypropylene bottles with excellent optical properties can be achieved when pre-blow is developed for more than 43% of the final bottle capacity. In earlier trials, we've learned that the clarity of polypropylene bottles is determined by a combination of several variables (injection fill rate, resin melt index, preform thickness, preform inner surface temperature, but also pre-blow conditions). If for one or another reason, one of these variables need to be held outside the normal operating range, an optimization of the pre-blow conditions becomes particularly important for addressing issues with poor bottle clarity. In this example, a significant reduction of the power of a specific infrared lamp is required to give the bottle the desired wall thickness distribution what created an undesirable haziness in the corresponding area of the bottle panel. This example illustrates how the use of certain pre-blow conditioned solved a significant transparency issue.

It is understood by one of ordinary skill in the art that the present discussion is a description of exemplary embodiments only, and is not intended as limiting the broader aspects of the present invention, which broader aspects are embodied in the exemplary constructions. The invention is shown by example in the claims.

Claims

1. A process for forming a plastic container having relatively low levels of haze by employing an effective mold filling rate having a value below a calculated critical threshold mold filling rate, said method comprising the steps of: (a) making a preform article having a given wall thickness (T) in a mold by: (i) providing a chemical composition comprising polypropylene, said chemical composition having a predetermined given melt flow index (MFI); (ii) calculating a critical mold filling rate using said given values for MFI and T, said critical mold filling rate being the maximum mold filling rate for which containers of acceptable levels of haze may be made; (iii) injecting said chemical composition into said mold at a predetermined mold filling rate, said predetermined mold filling rate being of a lesser value than said calculated critical mold filling rate; and (b) forming said preform article into a container having relatively low levels of haze.

2. The process of claim 1 wherein said mold is filled by providing said chemical composition through a valve gate, said valve gate having a diameter of about 1.5 mm.

3. The process of claim 2 wherein said side wall thickness of said preform article is between about 1.5 mm and about 3.5 mm.

4. The process of claim 2 wherein at a critical filling rate of about 10 grams/second said MFI is less than about 42.

5. The process of claim 1 wherein said critical filling rate is established by solving the following relationship with substituted values for MFI and T:

6. The process of claim 1 wherein said chemical composition further comprises a nucleating agent.

7. The process of claim 6 wherein said nucleating agent comprises a dibenzylidene sorbitol compound (DBS), or a derivative thereof.

8. The process of claim 6 wherein said nucleating agent comprises sodium 1,3-0-2,4-bis(4-methylbenzylidene) sorbitol and derivatives thereof.

9. The process of claim 6 wherein said nucleating agent comprises sodium benzoate and derivatives thereof.

10. The process of claim 6 wherein said nucleating agent comprises 1,2-cyclohexanedicarboxylate salts and derivatives thereof.

11. The process of claim 6 wherein said nucleating agent comprises aluminum 4-tert-butylbenzonate and derivatives thereof.

12. The process of claim 6 wherein said nucleating agent comprises metal salt(s) of cyclic phosphoric esters and derivatives thereof.

13. The process of claim 6 wherein said nucleating agent comprises bis(3,4-dialkylbenzylidene) sorbitol acetal or derivatives thereof.

14. The process of claim 6 wherein said nucleating agent comprises 1,3-O-2,4-bis(3,4-dimethylbenzylidene) sorbitol or derivatives thereof.

15. The process of claim 6 wherein said nucleating agent comprises disodium bicyclo[2.2.1]heptanedicarboxylate or derivatives thereof.

16. The process of claim 1 wherein said chemical composition comprises at least one species of polypropylene homopolymer.

17. The process of claim 1 wherein said chemical composition comprises a polypropylene random copolymer.

18. The process of claim 1 wherein said chemical composition comprises a polypropylene block copolymer.

19. The process of claim 1 wherein said forming step (b) includes a pre-blowing step, said pre-blowing step.

20. The process of claim 2 wherein said plastic containers are formed in a manufacturing operation at a rate of container production of greater than about 1200 containers per hour per mold.

21. The process of claim 2 wherein said container provides a haze to thickness ratio expressed as a percent haze/mils of less than about 0.05.

22. A process for forming a container having relatively low levels of haze by employing an effective mold filling rate having a value below a critical mold filling rate for a given MFI and preform wall thickness, said method comprising the steps of: (a) making a preform article having a wall thickness (T) in a mold by (i) providing a chemical composition comprising polypropylene, said chemical composition having a predetermined melt flow index (MFI); (ii) calculating a critical mold filling rate for a given MFI and T; (iii) injecting said chemical composition into said mold at a predetermined mold filling rate, said predetermined mold filling rate being of a lesser value than a said critical filling rate; and (b) blowing said preform article into a container, said container having relatively low levels of haze.

23. The process of claim 22 wherein said mold is filled by providing said chemical composition through a valve gate, said valve gate having a diameter of about 1.5 mm.

24. The process of claim 22 wherein said blowing step (b) is preceded by a pre-blow step.

25. The process of claim 22 wherein said preblow step provides a bottle volume after preblow, but before blowing, which is at least 40% of the final blown bottle volume.

26. A process for forming a preform article that is capable of being blown into a plastic container having relatively low levels of haze, the process employing an effective mold filling rate having a value below a critical mold filling rate for a given MFI and preform wall thickness, said method comprising the steps of making a preform article having a wall thickness (T) in a mold by: providing a chemical composition comprising polypropylene, said chemical composition having a predetermined melt flow index (MFI); calculating a critical mold filling rate for a given MFI and T; and injecting said chemical composition into said mold at a predetermined mold filling rate, said predetermined mold filling rate being of a lesser value than a said critical filling rate; thereby forming a preform article.

27. A process for forming a plastic container having relatively low levels of haze by employing an effective mold filling rate having a value below a calculated critical threshold mold filling rate, said method comprising the steps of: (a) making a preform article having a given wall thickness (T) in a mold by: (i) providing a chemical composition comprising polypropylene, said chemical composition having a predetermined given melt flow index (MFI); (ii) calculating a critical mold filling rate using said given values for MFI and T, said critical mold filling rate being the maximum mold filling rate for which containers of acceptable levels of haze may be made; (iii) injecting said chemical composition into said mold at a predetermined mold filling rate, said predetermined mold filling rate being of a lesser value than said calculated critical mold filling rate; and (b) forming said preform article into a container having relatively low levels of haze.

28. The process of claim 27 wherein said mold is filled by providing said chemical composition through a valve gate, said valve gate having a diameter of about 3.8 mm.

29. The process of claim 27 wherein said mold is filled by providing said chemical composition through a valve gate, said valve gate having a diameter of about 3.0 mm.

30. The process of claim 27 wherein said mold is filled by providing a gate diameter of about 2.5 mm.

31. The process of claim 27 wherein said mold is filled by providing a gate diameter of about 2.5 mm.

32. The process of any of claims 27 wherein said critical fill rate is correlated to said MFI value.

33. The process of claim 28 wherein at a critical filling rate of about 16 grams/second and said MFI is less than about 20.

34. The process of claim 27 wherein said mold is filled by providing said chemical composition through a valve gate, said valve gate having a diameter of about 3.0 mm.

35. The process of claim 27 wherein at a critical filling rate of about 13 grams/second said MFI is less than about 20.

36. The process of claim 27 wherein said mold is filled by providing a gate diameter of about 2.5 mm.

37. The process of claim 27 wherein at a critical filling rate of about 13 grams/second said MFI is less than about 20.

38. The process of claim 27 wherein said mold is filled by providing a gate diameter of about 2.0 mm.

39. The process of claim 27 wherein at a critical filling rate of about 12 grams/second said MFI is less than about 20.

40. The process of any of claims 27 wherein said critical fill rate is correlated to said MFI value.