WO2022221049A1

WO2022221049A1 - Processes for making improved polypropylene homopolymers, random copolymers, and impact copolymers

Info

Publication number: WO2022221049A1
Application number: PCT/US2022/022326
Authority: WO
Inventors: Zerong Lin; Antonios K. Doufas; Lindon John T. LIMPANGOG
Original assignee: Exxonmobil Chemical Patents Inc.
Priority date: 2021-04-15
Filing date: 2022-03-29
Publication date: 2022-10-20

Abstract

Processes for making polypropylene homopolymers, random copolymers, and/or impact copolymers. A process for making an impact copolymer can include polymerizing propylene, or copolymerizing propylene and at least one other α-olefin comonomer, in a first reactor system in the presence of (a) a solid catalyst component comprising a magnesium compound and a titanium compound; (b) an alkylzinc compound present in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 10,000; (c) hydrogen in an amount of about 500 mppm to about 20,000 mppm, based on the amount of propylene introduced to the first reactor system; (d) an organoaluminum compound; and (e) an external electron donor comprising an amino-silane donor, thereby producing a polypropylene homopolymer or random copolymer; and introducing the polypropylene homopolymer or random copolymer, additional propylene, and at least one other α-olefin comonomer to a second reactor system to produce an impact copolymer.

Description

PROCESSES FOR MAKING IMPROVED POLYPROPYLENE HOMOPOLYMERS, RANDOM COPOLYMERS, AND IMPACT COPOLYMERS CROSS-REFERENCE TO RELATED APPLICATIONS [0001] This application claims priority to U.S. Provisional Application number 63/175181, which was filed on April 15, 2021, and which is incorporated by reference herein in its entirety. FIELD [0002] Embodiments of the present invention generally relate to processes for making polypropylene homopolymers, random copolymers, and impact copolymers. More particularly, such embodiments relate to the addition of alkyl zinc during the polymerization process to produce polypropylene homopolymers, random copolymers, and/or impact copolymers having improved properties. BACKGROUND [0003] Impact copolymers (ICPs) are commonly used in a variety of applications where strength and impact resistance are desired, such as molded and extruded automobile parts, construction parts, rigid packaging, household appliances, luggage, and furniture. Propylene based ICP's are typically an intimate mixture of a continuous phase of a crystalline polypropylene polymer and a dispersed rubber phase of a secondary polymer, e.g., an ethylene copolymer. While these so-called ICP products have been produced by melt compounding the individual polymer components, multi-reactor technology makes it possible to produce them directly. This is accomplished by polymerizing propylene in a first reactor and transferring the polypropylene homopolymer (hPP) from the first reactor into a second reactor where the secondary copolymer is produced. [0004] ICP products with even higher stiffness, impact resistance, and melt flow rate (MFR) are in constant demand. However, the MFR of conventional ICP products is limited by the MFR capability of the hPP produced in the first reactor. One method commonly used to increase the MFR of the hPP and thus in turn increase the MFR of the ICP product has been to increase the concentration of hydrogen present in the first reactor. Unfortunately, hydrogen carried over from the first reactor to the second reactor can cause a decrease in the molecular weight of the resulting ICP such that the desired impact resistance cannot be obtained. [0005] A need therefore exists to develop a method for making hPP and thus ICP products with higher MFR without the need to increase the hydrogen concentration in the first reactor and with minimal process modifications. It is also desirable to produce ICP products having improved stiffness and impact resistance. SUMMARY [0006] Processes for making polypropylene homopolymers, random copolymers, and/or impact copolymers having improved properties are provided. In one or more embodiments, a process for making a polypropylene homopolymer can include polymerizing propylene in the presence of (a) a solid catalyst component comprising a magnesium compound and a titanium compound; (b) an alkylzinc compound present in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 20,000; (c) hydrogen in an amount of about 500 mppm to about 20,000 mppm, based on the amount of propylene present; (d) an organoaluminum compound; and (e) an external electron donor comprising an amino-silane donor. In other embodiments, a random copolymer can be made in the same manner as the polypropylene homopolymer except that the propylene can be copolymerized with at least one other α-olefin comonomer to produce the random copolymer. [0007] In one or more embodiments, a process for making an impact copolymer can include polymerizing propylene, or copolymerizing propylene and at least one other α-olefin comonomer, in a first reactor system in the presence of (a) a solid catalyst component comprising a magnesium compound and a titanium compound; (b) an alkylzinc compound present in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 10,000; (c) hydrogen in an amount of about 500 mppm to about 20,000 mppm, based on the amount of propylene introduced to the first reactor system; (d) an organoaluminum compound; and (e) an external electron donor comprising an amino-silane donor, thereby producing a polypropylene homopolymer or random copolymer comprising a melt flow rate greater than about 160 g/10 min and less than about 3,000 g/10 min, according to ASTM D1238; and introducing the polypropylene homopolymer of random copolymer, additional propylene, and at least one other α-olefin comonomer to a second reactor system to produce an impact copolymer. [0008] In one or more embodiments, a process for making a broad or bimodal polypropylene homopolymer can include polymerizing propylene in a first reactor system in the presence of (a) a solid catalyst component comprising a magnesium compound and a titanium compound; (b) an organoaluminum compound; and (c) an external electron donor, thereby producing a polypropylene homopolymer; and introducing the polypropylene homopolymer, additional propylene, hydrogen, and an alkylzinc compound to a second reactor system to produce broad or bimodal polypropylene homopolymer, the alkylzinc compound being present in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 10,000. [0009] In one or more embodiments, a process for making a broad or bimodal impact copolymer can include polymerizing propylene in a first reactor system in the presence of (a) a solid catalyst component comprising a magnesium compound and a titanium compound; (b) an alkylzinc compound present in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 10,000; (c) an organoaluminum compound; and (d) an external electron donor, thereby producing a polypropylene homopolymer; introducing the polypropylene homopolymer, additional propylene, hydrogen, and optionally an alkylzinc compound to a second reactor system to produce broad or bimodal polypropylene homopolymer, the alkylzinc compound being present in the second reactor system in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 10,000; and introducing the broad or bimodal polypropylene homopolymer, more propylene, and at least one other α-olefin comonomer to a third reactor system to produce a broad or bimodal impact copolymer. DETAILED DESCRIPTION [0010] It is to be understood that the following disclosure describes several exemplary embodiments for implementing different features, structures, and/or functions of the invention. Exemplary embodiments of components, arrangements, and configurations are described below to simplify the present disclosure; however, these exemplary embodiments are provided merely as examples and are not intended to limit the scope of the invention. Additionally, the present disclosure may repeat reference numerals and/or letters in the various exemplary embodiments and across the Figures provided herein. This repetition is for the purpose of simplicity and clarity and does not in itself dictate a relationship between the various exemplary embodiments and/or configurations discussed in the Figures. Moreover, the exemplary embodiments presented below can be combined in any combination of ways, i.e., any element from one exemplary embodiment can be used in any other exemplary embodiment, without departing from the scope of the disclosure. [0011] Additionally, certain terms are used throughout the following description and claims to refer to particular components. As one skilled in the art will appreciate, various entities can refer to the same component by different names, and as such, the naming convention for the elements described herein is not intended to limit the scope of the invention, unless otherwise specifically defined herein. Further, the naming convention used herein is not intended to distinguish between components that differ in name but not function. [0012] In the following discussion and in the claims, the terms “including” and “comprising” are used in an open-ended fashion, and thus should be interpreted to mean “including, but not limited to.” The phrase “consisting essentially of” means that the described/claimed composition does not include any other components that will materially alter its properties by any more than 5% of that property, and in any case does not include any other component to a level greater than 3 mass%. [0013] The term “or” is intended to encompass both exclusive and inclusive cases, i.e., “A or B” is intended to be synonymous with “at least one of A and B,” unless otherwise expressly specified herein. [0014] The indefinite articles “a” and “an” refer to both singular forms (i.e., “one”) and plural referents (i.e., one or more) unless the context clearly dictates otherwise. For example, embodiments using “an olefin” include embodiments where one, two, or more olefins are used, unless specified to the contrary or the context clearly indicates that only one olefin is used. [0015] The term “wt%” means percentage by weight, “vol%” means percentage by volume, “mol%” means percentage by mole, “ppm” means parts per million, and “mppm” and means parts per million on a molar basis. All concentrations herein, unless otherwise stated, are expressed on the basis of the total amount of the composition in question. [0016] The term “α-olefin” refers to any linear or branched compound of carbon and hydrogen having at least one double bond between the α and β carbon atoms. For purposes of this specification and the claims appended thereto, when a polymer or copolymer is referred to as including an α -olefin, e.g., poly- α -olefin, the α-olefin present in such polymer or copolymer is the polymerized form of the α-olefin. [0017] The term “polymer” refers to any two or more of the same or different repeating units/mer units or units. The term “homopolymer” refers to a polymer having units that are the same. The term “copolymer” refers to a polymer having two or more units that are different from each other, and includes terpolymers and the like. The term “terpolymer” refers to a polymer having three units that are different from each other. The term “different” as it refers to units indicates that the units differ from each other by at least one atom or are different isomerically. Likewise, the definition of polymer, as used herein, includes homopolymers, copolymers, and the like. By way of example, when a copolymer is said to have a “propylene” content of 10 wt% to 30 wt%, it is understood that the repeating unit/mer unit or simply unit in the copolymer is derived from propylene in the polymerization reaction and the derived units are present at 10 wt% to 30 wt%, based on a weight of the copolymer. [0018] The term “random copolymer” refers to a polypropylene polymer having repeating units of the α-olefin monomer(s) present in a random or statistical distribution in the polymer chain. The term “impact copolymer” refers a polymer having an α-olefin-propylene copolymer (rubber phase) dispersed in a continuous phase of polypropylene (crystalline phase). Also, the term “crystalline phase” refers to a phase of a polymer in which the polymer chains are arranged in ordered crystals. The terms “rubber phase” and “amorphous phase” can be used interchangeably and refer to a phase of a polymer in which the polymer chains are not arranged in ordered crystals. [0019] As used herein, “Mn” refers to the number average molecular weight of the different polymers in a polymeric material, “M_w” refers to the weight average molecular weight of the different polymers in a polymeric material, and “Mz” refers to the z average molecular weight of the different polymers in a polymeric material. Molecular weight distribution (MWD), also referred to as polydispersity index (PDI), is herein defined to be the ratio of Mw to Mn. Unless otherwise noted, all molecular weights (e.g., Mw, Mn, Mz) are reported in units of g/mol. Also, the term “bimodal” refers to a polymeric material having a MWD with two distinctive peaks, and the term “broad” refers to a polymeric material having a MWD that is greater than 5. [0020] Nomenclature of elements and groups thereof used herein are pursuant to the Periodic Table used by the International Union of Pure and Applied Chemistry after 1988. An example of the Periodic Table is shown in the inner page of the front cover of Advanced Inorganic Chemistry, 6th Edition, by F. Albert Cotton et al. (John Wiley & Sons, Inc., 1999). [0021] A detailed description will now be provided. Each of the appended claims defines a separate invention, which for infringement purposes is recognized as including equivalents to the various elements or limitations specified in the claims. Depending on the context, all references to the “invention” may in some cases refer to certain specific embodiments only. In other cases, it will be recognized that references to the “invention” will refer to subject matter recited in one or more, but not necessarily all, of the claims. Each of the inventions will now be described in greater detail below, including specific embodiments, versions and examples, but the inventions are not limited to these embodiments, versions or examples, which are included to enable a person having ordinary skill in the art to make and use the inventions, when the information in this disclosure is combined with publicly available information and technology. [0022] Processes for making polypropylene homopolymers (hPPs), random copolymer (RCPs), and impact copolymers (ICP) that have higher melt flow rates (MFRs) are disclosed herein. It has been surprisingly discovered that addition of an alkylzinc compound such as diethyl zinc during the hPP homopolymerization process and/or the RCP copolymerization process in the presence of a Ziegler-Natta catalyst can produce hPPs and/or RCPs having significantly higher MFRs. Thus, the amount of hydrogen used to produce hPPs and/or RCPs can be minimized. While the hPP homopolymerization and the RCP copolymerization processes can be performed in the presence of any external electron donor suitable for use with Ziegler-Natta catalysts, it has also been surprisingly discovered that amino-silane compounds used as the external electron donor results in the production of hPPs and RCPs with even higher MFRs. For example, hPPs and RCPs can now be produced via the processes provided herein that have MFRs greater than 160, 300, 500, 700, or even 900 g/10 min and less than 3,000 or 1,000 g/10 min, according to ASTM D1238 (230°C/2.16 kg). [0023] These inventive hPPs and RCPs having higher MFRs can be used to produce ICPs having higher MFRs without concern that the molecular weight and the impact resistance of the ICPs are compromised due to too much hydrogen. On the contrary, ICPs with more amorphous rubber and less crystalline content can be produced that exhibit better stiffness- impact balance. Also, there is no need to remove hydrogen between the hPP/RCP and the ICP production stages, which reduces production costs. [0024] Processes for making hPPs and ICPs having broad or bimodal molecular weight distribution (MWDs) are also provided herein. The hPP with broad or bimodal MWD can be prepared in a first reactor system in the presence of little or no hydrogen, followed by preparing ICP from the broad or bimodal hPP in a two-reactor system copolymerization process in the presence of an alkylzinc compound and additional hydrogen. Alternatively, little or no hydrogen can be used in reactor systems downstream from the first reactor system while more hydrogen can be added to the first reactor system along with an alkylzinc compound. Overall, less hydrogen is required to make the ICP having a broad or bimodal matrix than would otherwise be required in the absence of the alkylzinc compound. By “little or no”, it is meant that the amount of hydrogen present in the polymerization medium can range from 500, or 1000, or 2000 mppm to 8,000, or 8,500, or 9,000, or 9,200, or 9,400, or 20,000 mppm, with an upper limit of 10,000 mppm being preferred, based on the total amount of propylene being fed to the reactor system. ICPs formed according to these processes unexpectedly exhibit improved stiffness. [0025] In one or more embodiments, processes for making hPP can include polymerizing propylene in a first reactor system in the presence of a Ziegler-Natta (ZN) catalyst containing a magnesium compound and a titanium compound, an alkylzinc compound, hydrogen, an organoaluminum activator, and an external electron donor. The alkylzinc compound, the organoaluminum activator, and the external electron donor can be disposed in an inert solvent prior to being introduced to the reactor system. Examples of suitable inert solvents include n- butane, n-pentane, isopentane, n-hexane, n-heptane, n-oxtane, cyclohexane, toluene, and xylene. The alklyzinc compound can be present in an amount such that the zinc to titanium molar ratio ranges from 1 to 10,000, preferably from 5 to 5,000, or more preferably from 10 to 2,000. The amount of hydrogen present in the polymerization medium can range from 500, or 1000, or 2000 mppm to 8,000, or 8,500, or 9,000, or 9,200, or 9,400, or 20,000 mppm, with an upper limit of 10,000 mppm being preferred, based on the total amount of propylene being fed to the reactor system. Preferably, hydrogen is present to a level below the bubble point of the system. The ZN catalyst can include an internal electron donor commonly known in the art, including but not limited to a phthalate, a diether, a succinate, or combinations thereof. Examples of suitable external electron donors include organosilicon compounds such as dicyclopentyldimethoxysilane, n-propyltriethoxysilane, dicyclpentyldimethoxysilane, diethylaminotriethoxysilane, and combinations thereof. Amino-silane donors such as diethylaminotriethyoxysilane are preferred. A description of the compositions of different generation ZN catalysts (e.g.3^rd, 4^th, 5^th, etc.) that can be used for the polypropylene production processes disclosed herein can be found in E. Albizzati, G. Cecchin, J.C. Chadwick, G. Collina, U. Giannini, G. Morini, L. Noristi: “Ziegler-Natta Catalysts and Polymerizations” in N. Pasquini (ed.): Polypropylene Handbook, Hanser Publishers, Munich 2005, pp.15–106. [0026] In one or more embodiments, processes for making RCP are the same as the processes for making hPP except that the propylene can be copolymerized with at least one other α-olefin comonomer at conditions suitable for the copolymerization process. The at least one other α- olefin comonomer can be present in an amount ranging from 0.5 to 10.0 wt% based on the total amount of olefins being fed to the reactor system. [0027] The hPP or RCP made by the processes disclosed herein can be used to produce ICP. In particular, the hPP or RCP produced in the first reactor system, additional propylene, and at least one α-olefin comonomer can be introduced to a second reactor system at conditions suitable to copolymerize the propylene and the α-olefin comonomer. The amount of hydrogen present in the second reactor system can range from 500, or 1000, or 2000 mppm to 8,000, or 8,500, or 9,000, or 9,200, or 9,400, or 20,000 mppm, with an upper limit of 10,000 mppm being preferred, based on the total amount of olefins being fed to the second reactor system. Preferably, hydrogen is present to a level below the bubble point of the system. Titanocene can also be introduced to the first reactor system and/or the second reactor system at suitable amounts to control the MWD of the ICP product. Also, additional alkylzinc can be introduced to the second reactor system in addition to the first reactor system to further improve the MFR or the ICP product. The addition of alkylzinc to the process for producing ICP can result in a more amorphous rubber with less crystalline content, as exhibited by the relatively low amount of α-olefin comonomer present in the crystalline phase of the ICP, which can range from 1 to 10 wt%, preferably from 2 to 8 wt%, or more preferably from 3 to 6 wt%. The amount of α- olefin comonomer present in the rubber phase of the ICP can range from about 25 to 60 wt%, preferably from about 8 to 30 wt%, or more preferably from about 12 to 25 wt%. The amorphous phase content of the ICP can range from 5 to 40 wt%, preferably from 8 to 30 wt%, and more preferably from 12 to 25 wt%. The intrinsic viscosity (IV) ratio (IV of soluble fraction/IV of crystalline fraction) of the ICP can range from about 0.5 to about 6.0. “Soluble fraction” (“SF”) herein refers to the soluble (amorphous) portion of the rubber phase and amorphous portion of the matrix. The rest is the crystalline fraction (CF). The Crystex method described in the Examples can be used to determine the SF and CF. Also, the ICP can have a lower molecular weight (MW) in the range of from 40,000 g/mol to 150,000 g/mol, preferably from 70,000 g/mol to 120,000 g/mol, or more preferably from 85,000 g/mol to 105,000 g/mol. [0028] In one or more embodiments, broad or bimodal hPP can be made according to the same process as the hPP except that a second reactor system is employed downstream from the first reactor system and the alkyl zinc compound is introduced to the second reactor system instead of the first reactor system. Also, the hPP produced in the first reactor system, additional propylene, and hydrogen can be introduced to the second reactor system at conditions suitable for polymerization of the propylene. In this manner, broad or bimodal hPP can be produced in the second reactor system. Preferably, less hydrogen is introduced to the first reactor system than the second reactor system such that the amount of hydrogen present in the first reactor system ranges from 0 mppm to 10,000 mppm, based on the total amount of olefin feed. The amount of hydrogen introduced to the second reactor can range from 500, or 1000 , or 2000 mppm to 8,000, or 8,500, or 9,000, or 9,200, or 9,400, or 20,000 mppm, with an upper limit of 10,000 mppm being preferred, based on the total amount of olefin feed. Alternatively, more hydrogen could be introduced to the second reactor system than the first reactor system such that the amounts of hydrogen added to each reactor is reversed. The hydrogen is preferably present to a level below the bubble point of the system for both reactors. [0029] The broad or bimodal hPP can be further used to produce broad or bimodal ICP by employing a third reactor system downstream from the second reactor system. The broad or bimodal hPP produced in the second reactor system, hydrogen, more propylene, and optionally least one other α-olefin comonomer can be introduced to the third reactor system at conditions suitable for copolymerizing the propylene and the α-olefin comonomer, thereby producing broad or bimodal ICP. The amount of hydrogen introduced to the third reactor can range from 0 to 10,000 mppm, preferably from 0 to 5,000 mppm, or more preferably 500 to 2,000 mppm. The addition of alkylzinc to the process for producing broad or bimodal ICP can result in ICPs having higher rubber content, as exhibited by the relatively high amount of α-olefin comonomer present in the rubber phase of the ICP. The amount of α-olefin comonomer present in the rubber phase of the ICP can range from about 25 to 60 wt%, preferably from about 8 to 30 wt%, or more preferably from about 12 to 25 wt%. The amorphous phase content of the ICP can range from 5 to 40 wt%, preferably from 8 to 30 wt%, and more preferably from 12 to 25 wt%. ICPs produced in this manner can have a MFR ranging from 30 to 10,000, preferably from 40 to 500, or preferably from 60 to 200, according to ASTM D1238 (230°C/2.16 kg). The ICPs can also have a lower molecular weight (M_W) in the range from 40,000 g/mol to 150,000 g/mol, preferably from 70,000 g/mol to 120,000 g/mol, or more preferably from 85,000 g/mol to 105,000 g/mol. [0030] The alkylzinc compound disclosed herein can be represented by the general formula Zn R¹R², where R¹ and R² each represent a hydrocarbon group having 1 to 10 atoms. R¹ and R² can be the same group or different groups. Examples of suitable alkylzinc compounds include diethylzinc, dimethylzinc, di-n-propylzinc, diisopropylzinc, di-n-butylzinc, diisobutylzinc, and combinations thereof. [0031] The α-olefin comonomers disclosed herein can be or include C2-C20 α-olefins, preferably C2-C12 α-olefins. Examples of suitable α-olefins comonomers include ethylene, propylene, 1-butene, 1-pentene, 1-hexene, 1-heptene, 1-octene, 1-nonene, 1-decene, 1- undecene 1-dodecene, 1-tridecene, 1-tetradecene, 1-pentadecene, 1-hexadecene, 1- heptadecene, 1-octadecene, 1-nonadecene, 1-eicosene, 1-heneicosene, 1-docosene, 1- tricosene, 1-tetracosene, 1-pentacosene, 1-hexacosene, 1-heptacosene, 1-octacosene, 1- nonacosene, 1-triacontene, 4-methyl-1-pentene, 3-methyl-1-pentene, 5-methyl-1-nonene, 3,5,5-trimethyl-1-hexene, vinylcyclohexane, and vinylnorbornene. [0032] In any embodiment, the polymer formed can have a MWD in the range of from 2 to 10. In any embodiment, the polymer formed can be subjected to melt blowing to produce a meltblown fiber or fabric. The polymer used for this process can be in granule or pellet form, with the pellet form being preferred. The meltblown fiber and fabric can be made in a one-step process in which high-velocity air blows a molten thermoplastic resin from an extruder die tip onto a conveyor or takeup screen to form a fine fibered self-bonding web. The polymer can be fed as granules or pellets into an extruder where it can be mixed with additives in a masterbatch. Additives include stabilizers, peroxides, dyes, and other chemical agents. The resulting meltblown fiber or fabric can have MFR values as high as from 400 to 3,000, preferably from 700 to 2,000, or more preferably from 1,000 to 2,000, and the fiber or fabric can have a MWD ranging from 2 to 10. The meltblown product is preferably a reactor grade melt blown product, but peroxide vis-breaking can further be used if desired. Suitable melt blowing processes and/or applications are disclosed in U.S. Patent No. 10,077,516, U.S. Patent No. 7,081,299, and Melt Blown Process, Melt Blown Technology Today 7-12 (Miller Freeman Publ., Inc. 1989). [0033] In one type of meltblown process, metering pumps can be used to pump the molten polymer to a distribution system having a series of die tips, the polymer being in the molten state at some processing temperature. The die tip can be shaped such that the holes are in a straight line with high-velocity air impinging from each side. The die can have 0.38 mm diameter holes spaced at 10 to 16 per cm (25–40 per inch). The impinging high-velocity hot air can attenuate the filaments and form the desired fibers or microfibers. Immediately below or adjacent to the die, a large amount of ambient air can be drawn into the hot air stream containing the microfibers to cool the hot gas and solidify the microfibers onto a forming belt or other solid surface that is moving in such a manner as to create a continually renewed surface for the microfibers to contact and form a fabric or web. The processing temperature is one factor in the final fabric properties. The “optimal” processing temperature is one at which ideal properties of the fabric are achieved such as low shot with good hand and high barrier properties or good filtration properties. [0034] Other end use articles could be formed from the polymers produced by the processes disclosed herein, as would be apparent to those skilled in the art. For example, injection molded articles and articles formed via compounding could be formed from the polymers produced as disclosed herein. The Catalyst [0035] In any embodiment, the single catalyst is a Ziegler-Natta catalyst that preferably includes a solid titanium catalyst component comprising titanium as well as magnesium, halogen, at least one non-aromatic internal electron donor, and at least one external electron donor. The solid titanium catalyst component, also referred to as a Ziegler-Natta catalyst, can be prepared by contacting a magnesium compound, a titanium compound, and the internal electron donor. Examples of the titanium compound used in the preparation of the solid titanium catalyst component include tetravalent titanium compounds having the formula Ti(ORn)X4-n, wherein “R” is a hydrocarbyl radical, “X” is a halogen atom, and “n” is from 0 to 4. A hydrocarbyl radical is defined to be C1 to C20 radicals, C1 to C10 radicals, C6 to C20 radicals, or C7 to C21 radicals, any of which may be linear, branched, or cyclic where appropriate (aromatic or non-aromatic). [0036] Preferably, the halogen-containing titanium compound is a titanium tetrahalide, or titanium tetrachloride. Preferably, the magnesium compound to be used in the preparation of the solid titanium catalyst component includes a magnesium compound having reducibility (or capable of alkyl substitution) and/or a magnesium compound having no reducibility. Suitable magnesium compounds having reducibility can, for example, be magnesium compounds having a magnesium-carbon bond or a magnesium-hydrogen bond. Examples of useful magnesium compounds include dimethyl magnesium, diethyl-magnesium, dipropyl magnesium, dibutyl magnesium, diamyl magnesium, dihexyl magnesium, didecyl magnesium, magnesium ethyl chloride, magnesium propyl chloride, magnesium butyl chloride, magnesium hexyl chloride, magnesium amyl chloride, butyl ethoxy magnesium, ethyl butyl magnesium, and/or butyl magnesium halides. In combination with the magnesium compound, the titanium- based Ziegler-Natta catalyst is said to be supported, thus the solid part of the catalyst. [0037] In any embodiment, the Ziegler-Natta catalysts are used in combination with an activator, also referred to herein as a Ziegler-Natta activator. Compounds containing at least one aluminum-carbon bond in the molecule may be utilized as the activators, also referred to herein as an organoaluminum activator. Suitable organoaluminum compounds include organoaluminum compounds of the general formula R¹mAl(OR²)nHpXq, wherein R¹ and R² are identical or different, and each represents a C1 to C15 hydrocarbyl radical (alkyl or aryl), preferably a C1 to C4 alkyl; “X” represents a halogen atom; and “m” is 1, 2, or 3; “n” is 0, 1, or 2; “p” is 0, 1, 2, or 3; and “q” is 0, 1, or 2; and wherein m+n+p+q=3. Other suitable organoaluminum compounds include complex alkylated compounds of aluminum represented by the general formula M¹AlR¹4, wherein M¹ is lithium, sodium, or potassium, and R¹ is as defined above. Suitable examples of the organoaluminum compounds include trialkyl aluminums such as trimethyl aluminum, triethyl aluminum and tributyl aluminum; trialkenyl aluminums such as triisoprenyl aluminum; dialkyl aluminum alkoxides such as diethyl- aluminum ethoxide and dibutyl aluminum ethoxide; alkyl aluminum sesquialkoxides such as ethyl aluminum sesquiethoxide and butyl aluminum sesquibutoxide. [0038] Both internal and external electron donors are desirable for forming the Ziegler-Natta catalyst disclosed herein. The internal electron donors are typically part of the solid catalyst component, while the external electron donors are typically added separately from the solid catalyst component. More particularly, the internal electron donor can be used in the formation reaction of the catalyst as the transition metal halide is reacted with the metal hydride or metal alkyl. Examples of suitable internal electron donors include amines, amides, ethers, esters, ketones, nitriles, phosphines, stilbenes, arsines, phosphoramides, thioethers, thioesters, aldehydes, alcoholates, and salts of organic acids, any of which may include an aromatic group. [0039] In any embodiment, the one or more internal donors are non-aromatic. The non- aromatic internal electron donor can be or can include an aliphatic amine, amide, ester, ether, ketone, nitrile, phosphine, phosphoramide, thioethers, thioester, aldehyde, alcoholate, carboxylic acid, or combinations thereof. In any embodiment, the non-aromatic internal electron donor(s) comprise a substituted or unsubstituted C4 to C10 or C20 di-, tri-, or tetra- ether or glycol, a substituted or unsubstituted C4 to C10 or C20 carboxylic acid or carboxylic acid ester that may include one or more ether groups, or a combination of two or more such compounds. By “substituted” what is meant is that the compound may include groups such as hydroxides, amines, silanes, or a combination thereof. In any embodiment, the one or more compounds include secondary or tertiary carbon atoms (thus iso- or tert-hydrocarbon compounds). Particularly suitable internal electron donors include phthalates, diethers, p- ethoxy esters, succinates, or combinations thereof. [0040] In any embodiment, at least one, and in some embodiments two or more external electron donors are used in combination with the solid Ziegler-Natta catalyst component, as long as one of them is an amino-silane donor. External donors are preferably added to the polymerization reactors as a separate component along with the catalyst and activator. As used herein, an “amino-silane” donor is an external electron donor having at least one amine or alkylamine moiety and at least one silane, alkylsilane or siloxane moiety. In any embodiment, the external electron donors can be or can include an organic silicon compound of the general formula R¹4Si and/or R¹nSi(NR²2)4-n, wherein each R¹ is independently selected from hydrogen, C1 to C10 linear and branched alkyls and alkenes, C4 to C12 cycloalkyls and cycloalkenes, C5 to C14 aryls, C6 to C20 alkylaryls, C1 to C10 linear or branched alkoxys, C4 to C12 cycloalkoxys, C5 to C14 aryloxys, and C6 to C20 alkylaryloxys; preferably each R¹ is independently selected from C1 to C6 linear, branched and cyclic alkyls or alkoxys; and each R² is independently selected from hydrogen, C1 to C10 linear and branched alkyls and alkenes, C4 to C12 cycloalkyls and cycloalkenes, C5 to C14 aryls, and C6 to C20 alkylaryls; preferably each R² is independently selected from C1 to C5 linear or branched alkyls; and wherein “n” is 0, 1, 2, or 3, preferably 2 or 3, most preferably 3. [0041] Examples of the suitable amino-silane compounds and/or organosilicon compounds for use as external electron donors include dimethylaminotriethoxysilane, diethylaminotriethoxysilane, vinylethylaminotriethoxysilane, dipropylaminotriethoxysilane, dimethylaminotrimethoxysilane, dimethylaminotripropylsilane, diethylaminodicyclopentylmethoxysilane, diethylaminodimethoxycyclohexylsilane, dipropylaminovinyldimethoxysilane, trimethylmethoxysilane, trimethylethoxysilane, dimethyldimethoxysilane, dimethyldimethoxysilane, dimethyldiethoxysilane, diisopropyldiethoxysilane, t-butylmethyl-n-diethoxysilane, t-butylmethyldiethoxysilane, t- amylmethyldiethoxysilane, diphenyldimethoxysilane, phenylmethyldimethoxysilane, diphenyldiethoxysilane, bis-o-tolyldimethoxysilane, bis-m-tolyldimethoxysilane, bis-p- tolyldimethoxysilane, bis-p-tolyldimethoxysilane, bisethylphenyldimethoxysilane, dicyclohexyldiethoxysilane, cyclohexylmethyldimethoxysilane, cyclohexylmethyldiethoxysilane, ethyltrimethoxysilane, ethyltriethoxysilane, vinyltrimethoxysilane, methyltrimethoxysilane, n-propyltriethoxysilane, decyltrimethoxysilane, decyltriethoxysilane, phenyltrimethoxysilane, γ- chloropropyltrimethoxysilane, methyltriethoxysilane, ethyltriethoxysilane, vinyltriethoxysilane, t-butyltriethoxysilane, n-butyltriethoxysilane, isobutyltriethoxysilane, phenyltriethoxysilane, γ-aminopropyltriethoxysilane, chlorotriethoxysilane, vinyltributoxysilane, cyclohexyltrimethoxysilane, cyclohexyltriethoxysilane, 2- norbornanetriethoxysilane, 2-norbornanemethyldimethoxysilane, ethyl silicate, butylsilicate, trimethylphenoxysilane, methylallyloxysilane, vinyltris(β-methoxyethoxysilane), vinyltriacetoxysilane, dimethyltetraethoxydisiloxane, tetraethoxysilane, methylcyclohexyldimethoxysilane, propyltriethoxysilane, and/or dicyclopentyldimethoxysilane. [0042] Preferably, the external electron donor consists of only one or more amino-silane donors, and most preferably only one type of amino-silane donor. Different external electron donors can be added to the different reactors to affect the polypropylene properties such as making the polypropylene broad or bimodal in MFR, molecular weight, crystallinity, or some other property, but most preferably only one external electron donor is added throughout, and most preferably at the same concentration. In any embodiment the combined concentration of external electron donors can be present with the catalyst and olefin monomer(s) in the reactor to within a range from 5, or 10, or 20 ppm to 80, or 100, or 120 ppm based on the total olefin concentration. [0043] The concentration of the Ziegler-Natta catalyst in the polymerization system can be from 2, or 4, or 8 ppm to 20, or 40, or 60, or 100 ppm based on the total olefin concentration. The organoaluminum activator can be present in an amount sufficient to produce from 0.1 to 500 g, or more preferably from 0.3 to 300 g, of a polypropylene per gram of the titanium catalyst present, and can be present at from 0.1 to 100 moles, or more preferably from 0.5 to 50 moles, per mole of the titanium atom present in the catalyst component. Stated another way, the organoaluminum activator can be present to within a range from 10, or 20, or 40 ppm to 80, or 100, or 140, or 180, or 200 ppm, based on the total olefin concentration. Polymerization Processes [0044] Preferably, a slurry polymerization process is employed in the reactor for making hPP or RCP and a gas phase polymerization process is employed in the reactor(s) for making ICP or broad or bimodal ICP. Alternatively, a gas phase polymerization process could be employed in all reactors. [0045] The phrase “slurry polymerization process” refers to a process that handles propylene that is only partly dissolved or not dissolved at all in the polymerization medium, either olefin, solvent, or both, typically having at least 20 wt% propylene suspended or not dissolved. In a typical slurry polymerization process, catalyst components, solvent, olefins, alkyl zinc (when used), and hydrogen (when used) are passed under pressure to the reactor. Catalyst components can be passed to the polymerization reactor as a mixture in aliphatic hydrocarbon solvent, in oil, a mixture thereof, or as a dry powder. Most preferably, the polymerization process is otherwise carried out using propylene as the medium to carry the components and exchange heat with the environment. [0046] The phrase “gas phase polymerization process” refers to a process in which the propylene, any other olefins, and hydrogen (when used) are introduced to a reactor in the gas phase. The alkyl zinc can be dissolved in a solvent before being passed to the reactor. Catalyst components can be passed to the polymerization reactor in the same way as in the slurry polymerization process. Preferred Processes for Making ICPs [0047] The slurry polymerization process used in this invention is preferably a “bulk loop slurry process.” In any embodiment, the Ziegler-Natta catalyst, the activator, and the external electron donor is fed to a pre-polymerization reactor, either with or without a prior step to premix or “pre-contact” these components to activate the catalyst complex ahead of polymerization. The pre-polymerization reactor serves to start the reaction with the propylene monomer and/or other α-olefin comonomer at a low temperature (preferably 10°C to 30°C) to allow a small amount of polypropylene to grow around the catalyst particles to prevent fracturing, and thus create polypropylene fines which are difficult to process, when this catalyst with polypropylene is subsequently fed into the first main loop reactor along with more propylene monomer and/or α-olefin comonomer. However, in any embodiment, the pre- polymerization step can be absent, and the catalyst/activator/donors can be fed directly to the polymerization reactor(s). In any case, there may be one or two or more loop reactors in series or parallel, followed by separation equipment to remove remaining olefins from the polypropylene solids which can then be “finished” in either extrusion and pelletization equipment or loaded to containers directly as the material comes from the reactors. This is preferably when “additives” are combined with the ICP, if desired. [0048] The polymerization to produce the hPP or RCP (“hPP/RCP”) can be a “single stage” polymerization process, meaning that the olefin(s), catalyst components, dialkyl zinc compound, and optional hydrogen are contacted under the same or similar conditions throughout the production of the hPP/RCP, such as in a single reactor, or multiple reactors in parallel or series, held at a constant level of temperature, pressure, olefin concentration, and hydrogen concentration, where no parameter changes by more than +5%, or +10%. Thus, for example, a polymerization is single stage even if performed in two or more loop slurry reactors in parallel if the reactor conditions are held at a constant level. [0049] In any embodiment, hydrogen may be present in the reactor to modulate the molecular weight of the hPP/RCP being produced. In any embodiment, the hydrogen, if combined with the single catalyst during the polymerization, is combined at a constant level. This means that the total concentration of hydrogen in the reactor is held constant during the production of the hPP/RCP. In any embodiment, the level of hydrogen is kept at or below the bubble point, most preferably below the bubble point of the system. [0050] In any embodiment, the temperature of the reactor can be controlled by the rate of catalyst addition (rate of polymerization), the temperature of the olefin feed stream, and/or the use of heat transfer systems. For olefin polymerization, reactor temperatures can range from 50°C to 120°C or more while pressures can range from 2.1 to 8.3 MPaG. These process conditions favor in situ catalyst activation since high temperature enhances the solubility of catalysts and activators in propylene. The polymerization temperature is preferably at least 50, or 60, or 70 °C, or within a range from 50, or 60, or 70, or 80, or 90, or 100, or 120° C to 130, or 140, or 150, or 160, or 170° C. [0051] Prior to contacting with polymerization catalyst, the olefin monomers can be purified to remove potential catalyst poisons. The feedstock can be heated or cooled prior to delivery to the first and/or second reactors. [0052] The catalysts/activators/donors can be passed to one or more polymerization reactors in series or split between two or more reactors in parallel to produce the hPP/RCP. In slurry polymerization, the hPP/RCP produced remains dissolved or partially dissolved in the liquid olefin under reactor conditions. The catalyst can be passed to the reactor in solid form or as a slurry/suspension in an inert hydrocarbon solvent. Alternatively, the catalyst suspension can be premixed with the solvent in the feed stream for the polymerization reaction. Catalyst can be activated in-line or by an activator with which it is co-supported. In some instances, premixing is desirable to provide a reaction time for the catalyst components prior to entering the polymerization reactor, but this step may be absent. The catalyst activity is preferably 20,000 kg polypropylene per kg of catalyst or more, more preferably 50,000 kg polypropylene per kg of catalyst or more, even more preferably 100,000 kg polypropylene per kg of catalyst or more. [0053] Loop reactor systems typically include a single reactor or reactors in series or parallel configuration, such as that disclosed in US Patent Application No. 2007/0022768. The solvent/olefin flow in these reactors is typically maintained using pumps and/or pressure systems, and can operate continuously by having the feedstock enter at one point and extracting the forming hPP/RCP from another point, preferably downstream therefrom. The conditions of temperature, catalyst concentration, hydrogen concentration, and propylene and/or α-olefin comonomer concentrations can be the same or different in each loop reactor and can be tailored as necessary to suit the desired end product. In any embodiment, the solution polymerization process uses heat exchanger types of reactors for the polymerization. The reactors can be one or more shell and tube type of heat exchangers, or one or more spiral type of heat exchangers. [0054] Most preferably, no solvents are present in the bulk loop slurry process except for a minor amount used to initially suspend the catalyst and/or activator, and the system consists essentially of propylene and/or α-olefin comonomer as the polymerization medium and carrier of the forming polypropylene particles. In any embodiment the reactor pressure can be maintained and/or controlled using a pressurization drum, which is an apparatus containing liquid propylene and fluidly connected to the loop reactor, preferably the first loop, where the propylene is kept under pressure. The pressure of the propylene within the pressurization drum can be controlled by steam-heated propylene that can enter above a pool of liquid propylene in the drum. [0055] Thus, in any embodiment, the process includes contacting a catalyst with propylene and/or α-olefin comonomer (olefin(s)) in at least one slurry polymerization reactor to produce hPP/RCP, wherein the process further includes continuously separating the hPP/RCP from the remaining olefin(s) by first passing the hPP/RCP and remaining olefin(s) from the reactor(s) to a transfer line dryer to remove a portion of the olefin(s), preferably continuously, followed by passing the hPP/RCP and remaining olefin(s) to a high pressure separator (i.e., liquid-solid separator), whereby an amount of the remaining olefin(s) is further separated from a first separated hPP/RCP and directed to a recycle line to the reactor(s); directing the first separated hPP/RCP to a low pressure separator (i.e., gas-solid separator) whereby any remaining olefin(s) is further separated to obtain a second separated hPP/RCP and olefin(s) which is directed to a recycle line back to the reactor(s), wherein the second separated hPP/RCP is passed to a purge drum, then to an extruder to form finished pellets of hPP/RCP. In any embodiment, the first separated hPP/RCP and remaining olefin(s) can be passed to the low pressure separator through a second transfer line dryer to remove an amount of olefin(s) prior to entering the low pressure separator. [0056] Olefin(s) recovered from the high pressure separator can be recycled back to the first, second, or both loops in the reactor, with or without further compression. Also, olefin(s) recovered from the low pressure separator can also recycled back to the first, second, or both loops reactor, preferably with compression. Most preferably, no other separation means or steps to remove hPP/RCP from the olefin(s) are taken in either recycle stream. [0057] The recovered and mostly dried hPP/RCP can then be passed to another one or more second reactors to be further contacted with the remaining polymerization catalyst, external donor, and added α-olefin comonomer, preferably ethylene, thus forming an α-olefin-propylene copolymer (ICP), most preferably imbedded in the continuous phase of the hPP/RCP. Most preferably, the second reactor or reactors is a low pressure reactor that is operating at under 3.4 or 2.8 MPa such as a gas phase reactor GPR. [0058] Thus, the inventive process in any embodiment includes producing hPP/RCP, followed by transferring the hPP/RCP with still-active catalyst to one or more GPR's downstream, or with a second catalyst introduced in the GPR. During transfer, one or more separation steps can be included in order to remove liquid or gaseous olefin(s), diluents, or process feeds or gases from the hPP/RCP before being fed to the GPR. Most preferably, there is just one olefin(s)/polyolefin separation step. [0059] In the GPR, further propylene can be fed to the reactor along with at least one other α-olefin comonomer to produce an amorphous copolymer to complete the production of ICP. The reaction in the GPR can be controlled to produce copolymers with a broad variety of compositions and molecular weights, as well as the overall percentage of copolymer within the ICP produced. [0060] In any embodiment, the ratio of α-olefin comonomer to propylene can be varied to produce, in the example of ethylene-propylene ICP, from 5 or 15 wt % to 40, or 50, or 60, or 70 wt % ethylene (or other comonomer) in the ICP, based on the total weight of the ICP. This can be controlled via the feed rate of each reactant to the GPR. Also, in any embodiment a chain termination agent, for example hydrogen, or other reactants, such as propylene hydrogenation catalysts, can be additionally fed to the GPR to control the intrinsic viscosity of the ICP being formed. [0061] The amount of ICP produced in the GPR can be controlled in a variety of ways to produce ICP copolymer content in total polyolefin ranging from 2 to 30 wt % by weight, up to as high as 50 to 70 wt % based on the total weight of the ICP. These methods include, but are not limited to: (a) varying the mass of polyolefin within the reactor, the “bed” of polyolefin, to adjust the residence time and thus extent of reaction of the polyolefin within the reactor. This is typically controlled by the rate at which material is fed to the reactor relative to the rate at which polyolefin is removed from the reactor; and (b) utilizing catalyst control agents or poisons, either independently or in combination with bed mass, to alter catalyst activity thus controlling ethylene-propylene copolymer produced. [0062] The range of copolymers can be produced with polypropylene of broad molecular weight ranges, or of broad molecular weight distributions, or broad compositional distribution, or in any combination. Thus, the overall process allows for vast variation in final ICP composition and molecular weight combinations to produce polymers designed for many differing end uses. [0063] The operation of the GPR is described here. In any embodiment, polypropylene produced in the first stages, such as loop slurry reactors, can be passed through transfer line driers to heat the material as it passes to a olefin/polyolefin separation device such as a dust separator, preferably operating at a pressure at or near the pressure of the loop slurry reactors to avoid having to re-pressurize the olefin as the separated olefin recirculates to the loop reactors. The separated polypropylene preferably has less than 10, or 8, or 6, or 4 wt %, by weight of the polypropylene and propylene remaining. This dried polypropylene is transferred to the GPR, typically a vertical, cylindrical fluidized bed reactor having an expansion zone above the bed wherein the polypropylene is fed into the bottom or some section of the bed and gas flow rises through the bed up into the expansion zone. [0064] Once fed into the GPR, the polypropylene and forming ICP and other solid components can be kept in a fluidized state via one of the following methods or a combination thereof. In any embodiment, the gas can be recirculated from the GPR overhead to the bottom of the GPR at a high enough velocity that the polyolefin particles, or granules, or powder, etc. are fluidized by the flow of gas through the polyolefin bed. This velocity can be maintained high enough to fluidize the granules but not high enough to carry granules or significant quantities of dust or fines overhead and along with the recirculating gas stream. In any embodiment, the gas flow up the fluidized bed can be within a range from 500 or 600 klb/hr up to 1200, or 1400, or 1600, or 2000 klb/hr. [0065] Reduction of fines carryover can also be achieved via vessel design, where the top of the reactor may be of wider diameter than the bed-containing section, creating an expansion zone to allow further reduction in gas velocity as it flows overhead. The gas can then flow through a compressor or blower in series with one or more cooling exchangers and can then be distributed across the diameter at the bottom of the GPR via a perforated plate or via a conical bottom design of the reactor which provides for gas distribution as the gas flows, losing velocity as the cone opens upward. [0066] Also, in any embodiment, mechanical agitation of the polyolefin bed can be employed instead of, or in addition to, gaseous fluidization of the bed, which can also be maintained in a slightly wetted state via temperature control of the olefin monomer feeds added to the vessel. [0067] In any embodiment, heat of reaction in the GPR can be controlled via one of the following methods or a combination thereof: (a) cooling of the recirculating gas stream by passing the gas through a cooling exchanger after exiting the GPR overhead and either before or after reaching a compressor or blower that provides the motive force to recirculate the gas; (b) addition of pre-cooled feed streams to the reactor; (c) cooling jackets on the body of the reactor; or (d) controlled by one or more of these methods can range anywhere from 60°C or 65°C to 90°C or 100° C. [0068] In any embodiment, reactor pressure in the GPR can be controlled anywhere from 0.7 MPaG up to 2.1 or 3.4 MPaG, depending upon the monomers employed, by adjusting reaction rate, feed rate to and venting rate from the reactor. In any embodiment, the forming ICP can be removed from the vessel via piping from the bottom or side of the GPR, depending upon design specifics. This polyolefin “letdown” can be controlled by control valves in the piping allowing for flow control of the exiting polyolefin and gas. A slip-stream may or may not be passed through a cyclonic vessel to assist in removing some gas from the polyolefin stream while preventing removing smaller particle size polyolefin, or fines, from the GPR to help prevent wall and/or plate fouling. [0069] The process described above can be used to also produce broad or bimodal hPP and broad or bimodal ICP. In this embodiment, a third reactor is employed. The broad or bimodal hPP can be produced by polymerizing propylene in the first slurry-phase reactor and then introducing the hPP that is formed to a second GPR reactor along with additional propylene, hydrogen, and an alkylzinc compound to produce broad or bimodal hPP. This broad or bimodal hPP, propylene monomer, and an α-olefin comonomer can be introduced to a third GPR reactor to produce broad or bimodal ICP. The slurry-phase reactor and GPR reactors can be operated in the same manner as described above. [0070] In any embodiment, one or more additives can be introduced to any of the polymerization processes described herein as deemed appropriate by one skilled in the art. Examples of suitable additives for producing ICP are disclosed in U.S. Patent No. 8,076,419, the entirety of which is incorporated by reference herein. Examples: [0071] The foregoing discussion can be further described with reference to the following non-limiting examples. Polypropylene Homopolymers [0072] Polypropylene homopolymers (hPPs) were synthesized as follows (Examples 1-16). To a 2 L ZipperClave™ reactor (manufactured by Parker Hannifin Corp.) was introduced 1.0 mL of 1.0 M diethylzinc (DEZ) in hexanes, 1.0 mL of 1.0 M TEAL in hexanes, 1.0 mL of 0.1 M external electron donor in hexanes, 250 mmol hydrogen, and 1000 mL propylene. The agitation was started. 1.0 mL of 1.0 M TEAL in hexanes, 1.0 mL of 0.1 M external donor in hexanes, and 0.15 g of 5 wt% commercial Ziegler-Natta catalyst in mineral oil pre-contacted in a charge tube were flushed into the reactor with 250 mL propylene. Propylene polymerization was carried out at room temperature for 5 min. Then the reaction mixture was heated up from room temperature to 70°C and the polymerization reaction was carried out for 1 hr. At the end of propylene homopolymerization, volatiles were vented off. This procedure was repeated using five different Ziegler-Natta catalysts (A, B, C, D, and E) with different external electron donors. The following external electron donors were used: A1-donor was a mixture of 5 mol% dicyclopentyldimethoxysilane and 95 mol% n-propyltriethoxysilane; D- donor was dicyclopentyldimethoxysilane; and U-donor was diethylaminotriethoxysilane. For comparison purposes, the foregoing procedure was repeated using the same catalysts and external donors but in the absence of DEZ (Comparative Examples 1-8) [0073] Table 1 below gives the particular type of catalyst used and the particular donor used for each example and comparative example. Table 1 below also gives polymerization, including catalyst activity, and melt flow rate (MFR) data for Ex.1-16 and C.Ex.1-8. Catalyst activity herein was calculated as grams of polypropylene produced/grams of catalyst/hr. Table 2 below provides additional properties of the hPP formed in Ex.2-4 and 6 and C.Ex.2-3. The procedures used to determine these properties are provided at the end of the Examples. Table 1: Polymerization and MFR Data for Ex.1-16 and C.Ex.1-8 Example Catalyst Generic Donor DEZ Hydrogen Activity MFR Description (mmol) (mmol) (g/g/hr) (g/10

_{C.Ex.8 B} ^4th Generation, P_hthalate ^{U 0 250 29330 346.3}

^b 6 mg catalyst, 1.6 mmol TEAL, 0.16 mmol donor were used Table 2: Properties of hPP Produced in Ex.2-4 and 6 and C.Ex.2-3 M Flex Exampl n Mw Mz Mw/Mn M_z/M Modulu mmmm MR

[0074] As shown in Tables 1-2, the addition of DEZ to the reactor unexpectedly resulted in significantly higher MFR and lower Mw while maintaining similar catalyst activity, MWD, flex modulus and tacticity. The data in Table 1 also suggests that for a given target hPP MFR, a lower amount of H₂ concentration is needed in the slurry phase polymerization. resulting in less H2 carry over to the gas phase reactor in a commercial process. The results of Ex.8-10 indicate that hPP MFR can also be controlled by adjusting the H₂ amount used. [0075] The data in Table 1 also indicates that the use of U-donor, i.e., diethylaminotriethoxysilane, produced hPPs with higher MFR values than the use of the other external electron donors. Ex.13-16 and C.Ex.7-8 were specifically designed to compare the use of U-donor to D-donor. These examples indicate that the use of U-donor (an amino-silane donor) with DEZ gives much higher MFR in comparison with the use of D-donor with DEZ. Polypropylene Impact Copolymers [0076] Polypropylene impact copolymers (ICPs) were synthesized as follows. During first stage propylene homopolymerization, 0.8 mL of 1.0 M DEZ in hexanes, 0.8 mL of 1.0 M TEAL in hexanes, 0.8 mL of 0.1 M external electron donor in hexanes, 250 mmol hydrogen, and 1,000 mL propylene were introduced to a 2 L ZipperClave™ reactor. The agitation was started. 0.8 mL of 1.0 M TEAL in hexanes, 0.8 mL of 0.1 M external donor in hexanes, and 0.12 g of 5 wt% commercial Ziegler-Natta catalyst in mineral oil pre-contacted in a charge tube were flushed into the reactor with 250 mL propylene. Propylene polymerization was carried out at room temperature for 5 min. Then the reaction mixture was heated up from room temperature to 70 °C, and the polymerization reaction was carried out for 1 hr. At the end of propylene homopolymerization, volatiles were vented off. During second stage ethylene- propylene copolymerization, 40/60 molar ethylene and propylene gases and optionally hydrogen were added to reach 180 psig (1.2 MPaG) total pressure, and the reaction mixture was allowed to agitate for 1 hr at 70^oC. At the end of copolymerization, volatiles were vented off. This procedure was performed twice, once using Ziegler-Natta catalyst A with U-donor and once using Ziegler-Natta catalyst B with U-donor (Examples 17 and 18). For comparison purposes, the foregoing procedure was repeated using the same catalysts and external donors but in the absence of DEZ (Comparative Examples 9-10). [0077] Table 3 below provides the particular type of catalyst used for each example and comparative example as well as polymerization, including catalyst mileage, and MFR data for Ex.17-18 and C.Ex.9-10. Catalyst mileage herein refers to the relative activity of the catalyst with respect to baseline conditions (grams of hPP/grams of catalyst/hr). Table 4 below provides crystex data for the ICPs formed in Ex.17-18 and C.Ex.9-10. The procedures used to determine these properties are provided at the end of the Examples. Table 3: Polymerization and MFR Data for Ex.17-18 and C.Ex.9-10 Hydrogen E^{xam le Catal st Donor DEZ} (mmol) ^Mileage MFR

Example Ethylene (wt%) IV IV Ratio SF W_hol CF SF Whol CF SF (SF/CF) ^(wt%)

sulted in similar rubber amount (reflected in % soluble fraction (SF)) and %C2 (ethylene) in SF, but surprisingly lower %C2 in the crystal fraction (CF) and lower intrinsic viscosity (IV) ratio (SF/CF) relative to the case of no DEZ (C.Ex.10). This implies that in the case of catalyst B, the presence of DEZ surprisingly lead to a more amorphous rubber with less crystalline content, thus less blocky C2 (4.70% C2 for C.Ex.10 vs. 3.24% C2 for Ex.18) and lower IV ratio (4.5 for C.Ex.10 vs. 1.95 for Ex.8). Lower IV ratio can be advantageous for production of ICPs with better stiffness-impact balance, better paintability, higher gloss, an ability to produce transparent ICPs, or combinations of these performance attributes. Without intending to be limited by theory, the improved stiffness-impact balance is believed to be due to better rubber dispersion as a result of lower viscosity mis-match between matrix and EP rubber phases. For Ex.17, which utilized catalyst A, we observed that overall the %SF was similar in the presence of DEZ relative to the case without DEZ (C.Ex.9). However, the total %C2 for Ex. 17 was about 14 wt% less when DEZ was present than when no DEZ was present (C.Ex.9), which may suggest that DEZ unexpectedly results in ICPs with higher amorphous content (more C3-rich rubber). In addition, under the polymerization conditions runs for Ex.17, we observed that the IV ratio was lower in the presence of DEZ relative to the case of no DEZ (C.Ex.9). Broad or Bimodal Polypropylene Homopolymers [0079] Polypropylene homopolymers with broad or bimodal MWD were synthesized as follows. During first stage propylene homopolymerization, 0.8 mL of 1.0 M TEAL in hexanes, 0.8 mL of 0.1 M donor in hexanes, optional hydrogen, and 1,000 mL propylene were introduced to a 2 L ZipperClave™ reactor. The agitation was started. 0.8 mL of 1.0 M TEAL in hexanes, 0.8 mL of 0.1 M donor in hexanes and 0.12 g of 5 wt% Ziegler-Natta in mineral oil precontacted in a charge tube were flushed into the reactor with 250 mL propylene. Propylene polymerization was carried out at room temperature for 5 min. Then the reaction mixture was heated up from room temperature to 70°C, and the polymerization reaction was carried out for 0.5 hr. At the end of first stage propylene homopolymerization, volatiles were vented off. During second stage propylene homopolymerization, 0.8 mL of 1.0 M DEZ in hexanes, hydrogen, and 1,250 mL propylene were added to the reactor. The agitation was started. The reaction mixture was heated up from room temperature to 70°C, and the polymerization reaction was carried out for another 0.5 hr. At the end of second stage propylene homopolymerization, volatiles were vented off. This procedure was performed twice using Ziegler-Natta catalyst A with U-donor (Examples 19 and 20). For comparison purposes, the foregoing procedure was repeated using the same catalyst and external donor but in the absence of DEZ (Comparative Example 11). Table 1 below also provides polymerization and MFR data for Ex.19-20 and C.Ex.11. Table 5: Polymerization and MFR Data for Ex.19-20 and C.Ex.11 H^{ydrogen, mmol} ^{Exam le Catal st Donor DEZ 1}st 2^nd _Activity MFR

ch DEZ was present produced hPPs with similar MFR values but advantageously at lower hydrogen content during the second stage. Broad or Bimodal Polypropylene Impact Copolymers [0081] An impact copolymer having an hPP matrix with broad or bimodal MWD was synthesized as follows (Example 21). During first stage propylene homopolymerization, 0.8 mL of 1.0 M TEAL in hexanes, 0.8 mL of 0.1 M donor in hexanes, optional hydrogen, and 1,000 mL propylene was introduced to a 2 L ZipperClave™ reactor. The agitation was started. 0.8 mL of 1.0 M TEAL in hexanes, 0.8 mL of 0.1 M U-donor (described above) in hexanes and 0.12 g of 5 wt% commercial Ziegler-Natta catalyst A (described above) in mineral oil precontacted in a charge tube were flushed into the reactor with 250 mL propylene. Propylene polymerization was carried out at room temperature for 5 min. Then the reaction mixture was heated up from room temperature to 70 °C, and the polymerization reaction was carried out for 0.5 hr. At the end of first stage propylene homopolymerization, volatiles were vented off. During second stage propylene homopolymerization, 0.8 mL of 1.0 M DEZ in hexanes, 250 mmol hydrogen and 1250 mL propylene were added. The agitation was started. The reaction mixture was heated up from room temperature to 70 °C, and the polymerization reaction was carried out for another 0.5 hr. At the end of second stage propylene homopolymerization, volatiles were vented off. During third stage ethylene propylene copolymerization, 40/60 molar ethylene and propylene gases and optionally hydrogen were added to the reactor to reach 180 psig (1.2 MPaG) total pressure, and the reaction mixture was allowed to agitate for 1 hr at 70^oC. At the end of copolymerization, volatiles were vented off. For comparison purposes, the foregoing procedure was repeated using the same catalyst and external donor but in the absence of DEZ (Comparative Example 12). [0082] Table 6 below provides the polymerization and MFR data for Ex.21 and C.Ex.12. Table 7 below provides crystex data for the ICPs formed in Ex.21 and C.Ex.12. The procedures used to determine these properties are provided at the end of the Examples. Table 6: Polymerization and MFR Data for Ex.21 and C.Ex.12 E^{xample Catalyst Donor DEZ} Hydrogen, mmol Mileage MFR (_mmol) 1^st hPP 2^nd hPP 3^rd ICP (g/g) (g/10 min)

Example Ethylene (wt%) IV IV Ratio SF Whole CF SF Whole CF SF (SF/CF) (wt%)

ge (Ex.21) had higher rubber content based on %SF than the ICP produced without DEZ in the second stage (C.Ex.12). Ethylene contents were higher and IV ratios were lower for Ex.21 compared to C.Ex.12. Test Procedures [0084] The MFR was determined using ASTM D1238 (260°C/2.16 kg). [0085] Molecular weight distributions were characterized using Gel-Permeation Chromatography (GPC), also referred to as Size-Exclusion Chromatography (SEC). Molecular weights (Mw, Mn, Mz, and Mv) were determined using High-Temperature Gel-Permeation Chromatography equipped with a Differential Refractive Index Detector (DRI). Experimental details on the measurement procedure are described in the literature by T. Sun, P. Brant, R. R. Chance and W. W. Graessley, 34(19) MACROMOLECULES, 6812-6820 (2001) and in U.S. Pat. No.7,807,769. [0086] For each reactor granule sample, a dry blend of the ingredients (polypropylene, 1000 ppm AO Irganox^® 1010 commercially available from BASF, 1,000 ppm Irgafos^® 168 commercially available from BASF, and 1,000 ppm sodium benzoate nucleator) was prepared and homogenized by hand mixing. The dry blend was fed in the hopper of a Thermo-Prism 11 mm co-rotating twin screw extruder with L/D of 40, which is commercially available from Thermo Fischer Scientific. The reactor granule dry blends were extruded with the following temperature profile: 190 ^oC, 195 ^oC, 200 ^oC, 200 ^oC, 205 ^oC, 205 ^oC, 205 ^oC, 205 ^oC. The screw speed was 400 rpm and the feed rate was chosen at 65-75% setting. Extruder process conditions were adjusted, if needed, so that the melt temperature did not exceed 220 ^oC to avoid thermal/shear degradation. The extruder strands were passed through a VariCut Pelletizer 11mm commercially available from Thermo Fischer Scientific, which was adjutant to the extruder to produce polymer in pellet form. [0087] For the flexural modulus (Flex) measurements, pellets made on the aforementioned Thermo-Prism 11 twin screw extruder were used for injection molding on a Boy Injection Molding Machine, which is commercially available from BOY Machines, Inc., under standard injection molding protocol at 190 - 200°. Then the 1% secant flexural modulus was measured according to ASTM D790 with an Instron™ Tensile Machine (manufactured by Instron Corp.) at 23° C and a velocity of 1 mm/ min. [0088] Tacticity was determined by using ¹³C NMR (Carbon NMR) spectroscopy to measure meso pentads and stereo and regio defect concentrations in the polymers produced. Carbon NMR spectra were acquired with a 10-mm broadband probe on a Varian spectrometer having a ¹³C frequency of at least 100 MHz. The samples were prepared in 1,1,2,2-tetrachloroethane- d2 (TCE). Sample preparation (polymer dissolution) was performed at 140°C where 0.25 grams of polymer was dissolved in an appropriate amount of solvent to give a final polymer solution of 3 mL. In order to optimize chemical shift resolution, the samples were prepared without chromium acetylacetonate relaxation agent. [0089] Chemical shift assignments for the stereo defects (given as stereo pentads) can be found in the literature (L. Resconi, L. Cavallo, A. Fait, and F. Piemontesi, 100 CHEM. REV. 1253-1345 (2000)). The stereo pentads (e.g., mmmm, mmmr, mrm, etc.) can be summed appropriately to give a stereo triad distribution (mm, mr and rr) and the mole percentage diads (m and r). Three types of regio defects were quantified: 2,1-erythro, 2,1-threo and 3,1- insertion. The structures and peak assignments for these are also given in the reference by Resconi et al. The concentrations for all regio defects (punctuations) are given in terms of number of regio defects per 10,000 monomer units (DR). Accordingly, the concentration of stereo defects (punctuations) is given as the number of stereo defects per 10,000 monomer units (DS). The total number of defects per 10,000 monomers (Dtotal) is calculated as: Dtotal=DS+DR [0090] The average meso run length (MRL) represents the total number of propylene units (on the average) between defects (stereo and regio) based on 10,000 propylene monomers and is defined in this invention as follows: MRL = 10 , 000 D total [0091] This definition of MRL in this invention is based upon the number of structural chain punctuations or defects that result from propylene insertions that have occurred in a non-regular fashion (stereo and regio defects). It does not include the punctuations due to the presence of comonomer (e.g., ethylene in a polypropylene random copolymer). The regio defects each give rise to multiple peaks in the carbon NMR spectrum, and these are all integrated and averaged (to the extent that they are resolved from the other peaks in the spectrum) to improve the measurement accuracy. The chemical shift offsets of the resolvable resonances used in the analysis are tabulated in U.S. Pat. No. 7,807,769. The average integral for each defect is divided by the integral for one of the main propylene signals (CH3, CH, CH2) and multiplied by 10,000 to determine the defect concentration per 10,000 monomers. [0092] Crystex (crystallization extraction), developed by PolymerChar, is a new and fully automated analytical approach for separating and analyzing the amorphous (SF) and crystalline phases (CF) of ICPs as described in L. Jeremic et al. “Rapid characterization of high-impact ethylene–propylene copolymer composition by crystallization extraction separation: comparability to standard separation methods”, International Journal of Polymer Analysis”, Vol, 25, No 8, 581-596 (2020). [0093] The Crystex data (SF and CF) for the ICPs was determined via the Crystex QC instrument manufactured by Polymer Char of Valencia, Spain using the following procedure. A sample of 2 g of polymer was dissolved in 200 mL of 1,2,4-trichlorobenzene (TCB) at 175^oC. During the first injection, the aliquot of the whole sample was eluted to the detectors at high temperature, and the intrinsic viscosity IV (dl/g) and the wt% of co-monomer (typically ethylene, C2) of the total polymer were measured through a built-in dual capillary viscometer and infrared detector, respectively. During the second injection, the polymer solution or an aliquot of the same was subsequently crystallized by decreasing the temperature to 40^oC, leading to separation of the amorphous portion (SF) and crystalline portion (CF) of the (total) impact copolymer polypropylene. By measuring the concentration of the initial polymer solution and the concentration of the solution after crystallization via a concentration detector, the amount of amorphous fraction (SF) was determined. In addition, the IV (dl/g) and the wt% of co-monomer (typically ethylene) of the SF were measured through the built-in dual capillary viscometer and infrared detector, respectively. After re-dissolution of the CF (non-SF at 40 ^oC in TCB) in TCB 165^oC, the amount of CF and the respective IV and wt% of co-monomer (C2) of the CF were determined. [0094] As mentioned previously, the quantification of the SF and CF as well as the determination of ethylene content (C2) were achieved by means of an infrared detector (IR4), where the combination of the IR4 detector and an online 2-capillary viscometer was used for the determination of the IV. Details for the calibration procedures of the IR4 and on-line viscometer detector and method of determination of the IV ratio can be found in the article of L. Jeremic et al. “Rapid characterization of high-impact ethylene–propylene copolymer composition by crystallization extraction separation: comparability to standard separation methods”, International Journal of Polymer Analysis”, Vol, 25, No 8, 581-596 (2020). The IV ratio was determined to be the IV of SF/the IV of CF. Listing of Embodiments [0095] This disclosure may further include any one or more of the following non-limiting embodiments: [0096] 1. A process for making a polypropylene homopolymer, comprising: polymerizing propylene in the presence of (a) a solid catalyst component comprising a magnesium compound and a titanium compound; (b) an alkylzinc compound present in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 20,000; (c) hydrogen in an amount of about 500 mppm to about 20,000 mppm, based on the amount of propylene present; (d) an organoaluminum compound; and (e) an external electron donor comprising an amino-silane donor, thereby producing the polypropylene homopolymer. [0097] 2. The process of embodiment 1, wherein the polypropylene homopolymer has a melt flow rate greater than about 160 g/10 min and less than about 3,000 g/10 min, according to ASTM D1238. [0098] 3. A process for making an impact copolymer, comprising: polymerizing propylene in a first reactor system in the presence of (a) a solid catalyst component comprising a magnesium compound and a titanium compound; (b) an alkylzinc compound present in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 10,000; (c) hydrogen in an amount of about 500 mppm to about 20,000 mppm, based on the amount of propylene introduced to the first reactor system; (d) an organoaluminum compound; and (e) an external electron donor comprising an amino-silane donor, thereby producing a polypropylene homopolymer comprising a melt flow rate greater than about 160 g/10 min and less than about 3,000 g/10 min, according to ASTM D1238; and introducing the polypropylene homopolymer, additional propylene, and at least one other α-olefin comonomer to a second reactor system to produce an impact copolymer. [0099] 4. The process of embodiment 3, wherein the solid catalyst component further comprises an internal electron donor comprising a phthalate, a diether, a succinate, or combinations thereof, and wherein the external electron donor comprises diethylaminotriethoxysilane. [00100] 5. The process of embodiment 3 or 4, wherein the zinc to titanium molar ratio ranges from about 5 to about 5,000, wherein a slurry phase polymerization process is used in the first reactor system and a gas phase polymerization process is used in the second reactor system, and wherein hydrogen is introduced to the second reactor system in an amount up to about 20,000 mppm, based on the total amount of olefins introduced to the second reactor system. [00101] 6. The process of embodiments 3 to 5, further comprising introducing titanocene to the first reactor system for the polymerization process; or introducing an additional alkylzinc compound, titanocene, or a combination thereof to the second reactor system for the copolymerization process. [00102] 7. The process of embodiments 3 to 6, wherein the impact copolymer comprises a rubber phase dispersed in a polypropylene crystalline phase, wherein an amount of soluble fraction in the impact copolymer ranges from about 5 wt% to about 40 wt%, wherein the at least one other α-olefin comonomer in the polypropylene crystalline phase is from about 1 wt% to about 10 wt%, and the at least one other α-olefin comonomer in the soluble fraction is from about 25 wt% to about 60 wt%, and wherein the impact copolymer has a melt flow rate of about 30 to about 1,000, as measured by ASTM D1238, and an intrinsic viscosity ratio of about 0.5 to about 6.0. [00103] 8. A process for making a random copolymer, comprising: copolymerizing propylene and at least one other α-olefin comonomer in a reactor system in the presence of (a) a solid catalyst component comprising a magnesium compound and a titanium compound; (b) an alkylzinc compound present in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 20,000; (c) hydrogen in an amount of about 500 mppm to about 20,000 mppm based on the total amount of olefins introduced to the reactor system; (d) an organoaluminum compound; and (e) an external electron donor comprising an amino-silane donor, thereby producing a random copolymer. [00104] 9. The process of embodiment 8, wherein the at least one other α-olefin comonomer introduced to the reactor system ranges from about 0.5 wt% to about 10.0 wt%, based on the total weight of olefins introduced to the reactor system. [00105] 10. The process of embodiment 8 or 9, wherein the random copolymer has a melt flow rate greater than about 160 g/10 min and less than about 3,000 g/10 min, according to ASTM D1238. [00106] 11. A process for making an impact copolymer, comprising: copolymerizing propylene and at least one other α-olefin comonomer in a first reactor system in the presence of (a) a solid catalyst component comprising a magnesium compound and a titanium compound; (b) an alkylzinc compound present in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 10,000; (c) hydrogen in an amount of about 500 mppm to about 20,000 mppm based on the total amount of olefins introduced to the first reactor system; (d) an organoaluminum compound; and (e) an external electron donor comprising an amino- silane donor, thereby producing a random copolymer comprising a melt flow rate greater than about 160 and less than about 3,000, according to ASTM D1238; and introducing the random copolymer, additional propylene, and the at least one other α-olefin comonomer to a second reactor system to produce an impact copolymer. [00107] 12. The process of embodiment 11, wherein the solid catalyst component further comprises an internal electron donor comprising a phthalate, a diether, a succinate, or combinations thereof, and wherein the external electron donor comprises diethylaminotriethoxysilane. [00108] 13. The process of embodiment 11 or 12, wherein the zinc to titanium molar ratio ranges from about 5 to about 5,000 or from about 10 to about 2,000, wherein a slurry phase polymerization process is used in the first reactor system and a gas phase polymerization process is used in the second reactor system, and wherein hydrogen is introduced to the second reactor system in an amount up to about 20,000 mppm, based on the total amount of olefins introduced to the second reactor system. [00109] 14. The process of embodiments 11 to 13, further comprising introducing titanocene to the first reactor system with the propylene and the at least one other comonomer; or introducing additional alkylzinc compound, titanocene, or a combination thereof to the second reactor system with the random copolymer, the additional propylene, and the at least one other α-olefin. [00110] 15. The process of embodiments 11 to 14, wherein the impact copolymer comprises a rubber phase dispersed in a random copolymer crystalline phase, wherein an amount of soluble fraction in the impact copolymer ranges from about 5 wt% to about 40 wt%, wherein the at least one other α-olefin comonomer in the crystalline phase is from about 1 wt% to about 10 wt%, and the at least one other α-olefin comonomer in the soluble fraction is from about 25 wt% to about 60 wt%, and wherein the impact copolymer has a melt flow rate of about 30 to about 1,000, as measured by ASTM D1238, and an intrinsic viscosity ratio of about 0.5 to about 6.0. [00111] 16. A process for making a broad or bimodal polypropylene homopolymer, comprising: polymerizing propylene in a first reactor system in the presence of (a) a solid catalyst component comprising a magnesium compound and a titanium compound; (b) an organoaluminum compound; and (c) an external electron donor, thereby producing a polypropylene homopolymer; and introducing the polypropylene homopolymer, additional propylene, hydrogen, and an alkylzinc compound to a second reactor system to produce broad or bimodal polypropylene homopolymer, the alkylzinc compound being present in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 10,000. [00112] 17. The process of embodiment 16, wherein the solid catalyst component further comprises an internal electron donor comprising a phthalate, a diether, a succinate, or combinations thereof, and wherein the external electron donor comprising an amino-silane donor. [00113] 18. The process of embodiment 16 or 17, wherein the zinc to titanium molar ratio ranges from about 5 to about 5,000 or from about 10 to about 2,000, wherein a slurry phase polymerization process is used in the first reactor system and a gas phase polymerization process is used in the second reactor system, wherein hydrogen is introduced to the first reactor system in an amount up to about 10,000 mppm, based on the total amount of olefins introduced to the first reactor system, and wherein hydrogen is introduced to the second reactor system in amount of about 500 mppm to about 20,000 mppm, based on the total amount of olefins introduced to the second reactor system. [00114] 19. A process for making a broad or bimodal impact copolymer, comprising: polymerizing propylene in a first reactor system in the presence of a solid catalyst component comprising a magnesium compound and a titanium compound; (b) an alkylzinc compound present in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 10,000; (c) an organoaluminum compound; and (d) an external electron donor, thereby producing a polypropylene homopolymer; introducing the polypropylene homopolymer, additional propylene, hydrogen, and optionally an alkylzinc compound to a second reactor system to produce broad or bimodal polypropylene homopolymer, the alkylzinc compound being present in the second reactor system in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 10,000; and introducing the broad or bimodal polypropylene homopolymer, more propylene, and at least one other α-olefin comonomer to a third reactor system to produce a broad or bimodal impact copolymer. [00115] 20. The process of embodiment 19, wherein the solid catalyst component further comprises an internal electron donor comprising a phthalate, a diether, a succinate, or combinations thereof, and wherein the external electron donor comprising an amino-silane donor. [00116] 21. The process of embodiment 19 or 20, wherein the zinc to titanium molar ratio ranges from about 5 to about 5,000 or from about 10 to about 2,000, wherein a slurry phase polymerization process is used in the first reactor system and a gas phase polymerization process is used in the second reactor system, wherein hydrogen is introduced to the first reactor system in an amount up to about 10,000 mppm, based on the total amount of olefins introduced to the first reactor system, and wherein hydrogen is introduced to the second reactor system in amount of from about 500 mppm to about 20,000 mppm, based on the total amount of olefins introduced to the second reactor system, and wherein hydrogen is introduced to the third reactor in an amount of from about 0 mppm to about 10.000 mppm. [00117] 22. The process of embodiments 19 to 21, wherein the zinc to titanium molar ratio ranges from about 5 to about 5,000 or from about 10 to about 2,000, wherein a slurry phase polymerization process is used in the first reactor system and a gas phase polymerization process is used in the second reactor system, wherein hydrogen is introduced to the first reactor system in amount of from about 500 mppm to about 20,000 mppm, based on the total amount of olefins introduced to the first reactor system, and wherein hydrogen is introduced to the second reactor system in an amount up to about 10,000 mppm, based on the total amount of olefins introduced to the second reactor system, and wherein hydrogen is introduced to the third reactor system in an amount of from about 0 mppm to about 10.000 mppm. [00118] 23. The process of embodiments 19 to 22, wherein the broad or bimodal impact comprises a rubber phase dispersed in a broad or bimodal polypropylene homopolymer crystalline phase or in a broad or bimodal random copolymer polypropylene crystalline phase. wherein an amount of soluble fraction in the impact copolymer ranges from about 5 wt% to about 40 wt%, wherein the at least one other α-olefin comonomer in the crystalline phases is from about 1 wt% to about 10 wt%, and the at least one other α-olefin comonomer in the soluble fraction is from about 25 wt% to about 60 wt%, and wherein the impact copolymer has a melt flow rate of about 30 to about 1,000, as measured by ASTM D1238. [00119] 24. A process for melt blowing the homopolymer or copolymer of embodiments 2, 7, 10, 15, or 22. [00120] 25. A fiber or fabric made from the homopolymer or copolymer of embodiments 2, 7, 10, 15, or 22. [00121] Certain embodiments and features have been described using a set of numerical upper limits and a set of numerical lower limits. It should be appreciated that ranges including the combination of any two values, e.g., the combination of any lower value with any upper value, the combination of any two lower values, and/or the combination of any two upper values are contemplated unless otherwise indicated. Certain lower limits, upper limits and ranges appear in one or more claims below. All numerical values are "about" or "approximately" the indicated value, and take into account experimental error and variations that would be expected by a person having ordinary skill in the art. [00122] Various terms have been defined above. To the extent a term used in a claim is not defined above, it should be given the broadest definition persons in the pertinent art have given that term as reflected in at least one printed publication or issued patent. Furthermore, all patents, test procedures, and other documents cited in this application are fully incorporated by reference to the extent such disclosure is not inconsistent with this application and for all jurisdictions in which such incorporation is permitted. [00123] While the foregoing is directed to embodiments of the present invention, other and further embodiments of the invention may be devised without departing from the basic scope thereof, and the scope thereof is determined by the claims that follow.

Claims

CLAIMS: What is claimed is: 1. A process for making a polypropylene homopolymer, comprising: polymerizing propylene in the presence of (a) a solid catalyst component comprising a magnesium compound and a titanium compound; (b) an alkylzinc compound present in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 20,000; (c) hydrogen in an amount of about 500 mppm to about 20,000 mppm, based on the amount of propylene present; (d) an organoaluminum compound; and (e) an external electron donor comprising an amino-silane donor, thereby producing the polypropylene homopolymer. 2. The process of claim 1, wherein the polypropylene homopolymer has a melt flow rate greater than about 160 g/10 min and less than about 3,000 g/10 min, according to ASTM D1238. 3. A process for making an impact copolymer, comprising: polymerizing propylene in a first reactor system in the presence of (a) a solid catalyst component comprising a magnesium compound and a titanium compound; (b) an alkylzinc compound present in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 10,000; (c) hydrogen in an amount of about 500 mppm to about 20,000 mppm, based on the amount of propylene introduced to the first reactor system; (d) an organoaluminum compound; and (e) an external electron donor comprising an amino-silane donor, thereby producing a polypropylene homopolymer comprising a melt flow rate greater than about 160 g/10 min and less than about 3,000 g/10 min, according to ASTM D1238; and introducing the polypropylene homopolymer, additional propylene, and at least one other α-olefin comonomer to a second reactor system to produce an impact copolymer.

4. The process of claim 3, wherein the solid catalyst component further comprises an internal electron donor comprising a phthalate, a diether, a succinate, or combinations thereof, and wherein the external electron donor comprises diethylaminotriethoxysilane. 5. The process of claim 3, wherein the zinc to titanium molar ratio ranges from about 5 to about 5,000, wherein a slurry phase polymerization process is used in the first reactor system and a gas phase polymerization process is used in the second reactor system, and wherein hydrogen is introduced to the second reactor system in an amount up to about 20,000 mppm, based on the total amount of olefins introduced to the second reactor system. 6. The process of claim 3, further comprising introducing titanocene to the first reactor system for the polymerization process; or introducing an additional alkylzinc compound, titanocene, or a combination thereof to the second reactor system for the copolymerization process. 7. The process of claim 3, wherein the impact copolymer comprises a rubber phase dispersed in a polypropylene crystalline phase, wherein an amount of soluble fraction in the impact copolymer ranges from about 5 wt% to about 40 wt%, wherein the at least one other α- olefin comonomer in the polypropylene crystalline phase is from about 1 wt% to about 10 wt%, and the at least one other α-olefin comonomer in the soluble fraction is from about 25 wt% to about 60 wt%, and wherein the impact copolymer has a melt flow rate of about 30 to about 1,000, as measured by ASTM D1238, and an intrinsic viscosity ratio of about 0.5 to about 6.0. 8. A process for making a random copolymer, comprising: copolymerizing propylene and at least one other α-olefin comonomer in a reactor system in the presence of (a) a solid catalyst component comprising a magnesium compound and a titanium compound; (b) an alkylzinc compound present in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 20,000; (c) hydrogen in an amount of about 500 mppm to about 20,000 mppm based on the total amount of olefins introduced to the reactor system; (d) an organoaluminum compound; and (e) an external electron donor comprising an amino-silane donor, thereby producing a random copolymer. 9. The process of claim 8, wherein the at least one other α-olefin comonomer introduced to the reactor system ranges from about 0.5 wt% to about 10.0 wt%, based on the total weight of olefins introduced to the reactor system. 10. The process of claim 8, wherein the random copolymer has a melt flow rate greater than about 160 g/10 min and less than about 3,000 g/10 min, according to ASTM D1238. 11. A process for making an impact copolymer, comprising: copolymerizing propylene and at least one other α-olefin comonomer in a first reactor system in the presence of (a) a solid catalyst component comprising a magnesium compound and a titanium compound; (b) an alkylzinc compound present in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 10,000; (c) hydrogen in an amount of about 500 mppm to about 20,000 mppm based on the total amount of olefins introduced to the first reactor system; (d) an organoaluminum compound; and (e) an external electron donor comprising an amino-silane donor, thereby producing a random copolymer comprising a melt flow rate greater than about 160 and less than about 3,000, according to ASTM D1238; and introducing the random copolymer, additional propylene, and the at least one other α- olefin comonomer to a second reactor system to produce an impact copolyme^r. 12. The process of claim 11, wherein the solid catalyst component further comprises an internal electron donor comprising a phthalate, a diether, a succinate, or combinations thereof, and wherein the external electron donor comprises diethylaminotriethoxysilane. 13. The process of claim 11, wherein the zinc to titanium molar ratio ranges from about 5 to about 5,000 or from about 10 to about 2,000, wherein a slurry phase polymerization process is used in the first reactor system and a gas phase polymerization process is used in the second reactor system, and wherein hydrogen is introduced to the second reactor system in an amount up to about 20,000 mppm, based on the total amount of olefins introduced to the second reactor system. 14. The process of claim 11, further comprising introducing titanocene to the first reactor system with the propylene and the at least one other comonomer; or introducing additional alkylzinc compound, titanocene, or a combination thereof to the second reactor system with the random copolymer, the additional propylene, and the at least one other α-olefin. 15. The process of claim 11, wherein the impact copolymer comprises a rubber phase dispersed in a random copolymer crystalline phase, wherein an amount of soluble fraction in the impact copolymer ranges from about 5 wt% to about 40 wt%, wherein the at least one other α-olefin comonomer in the crystalline phase is from about 1 wt% to about 10 wt%, and the at least one other α-olefin comonomer in the soluble fraction is from about 25 wt% to about 60 wt%, and wherein the impact copolymer has a melt flow rate of about 30 to about 1,000, as measured by ASTM D1238, and an intrinsic viscosity ratio of about 0.5 to about 6.0. 16. A process for making a broad or bimodal polypropylene homopolymer, comprising: polymerizing propylene in a first reactor system in the presence of (a) a solid catalyst component comprising a magnesium compound and a titanium compound; (b) an organoaluminum compound; and (c) an external electron donor, thereby producing a polypropylene homopolymer; and introducing the polypropylene homopolymer, additional propylene, hydrogen, and an alkylzinc compound to a second reactor system to produce broad or bimodal polypropylene homopolymer, the alkylzinc compound being present in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 10,000. 17. The process of claim 16, wherein the solid catalyst component further comprises an internal electron donor comprising a phthalate, a diether, a succinate, or combinations thereof, and wherein the external electron donor comprising an amino-silane donor.

18. The process of claim 16, wherein the zinc to titanium molar ratio ranges from about 5 to about 5,000 or from about 10 to about 2,000, wherein a slurry phase polymerization process is used in the first reactor system and a gas phase polymerization process is used in the second reactor system, wherein hydrogen is introduced to the first reactor system in an amount up to about 10,000 mppm, based on the total amount of olefins introduced to the first reactor system, and wherein hydrogen is introduced to the second reactor system in amount of about 500 mppm to about 20,000 mppm, based on the total amount of olefins introduced to the second reactor system. 19. A process for making a broad or bimodal impact copolymer, comprising: polymerizing propylene in a first reactor system in the presence of (a) a solid catalyst component comprising a magnesium compound and a titanium compound; (b) an alkylzinc compound present in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 10,000; (c) an organoaluminum compound; and (d) an external electron donor, thereby producing a polypropylene homopolymer; introducing the polypropylene homopolymer, additional propylene, hydrogen, and optionally an alkylzinc compound to a second reactor system to produce broad or bimodal polypropylene homopolymer, the alkylzinc compound being present in the second reactor system in an amount such that the zinc to titanium molar ratio ranges from about 1 to about 10,000; and introducing the broad or bimodal polypropylene homopolymer, more propylene, and at least one other α-olefin comonomer to a third reactor system to produce a broad or bimodal impact copolymer. 20. The process of claim 19, wherein the zinc to titanium molar ratio ranges from about 5 to about 5,000 or from about 10 to about 2,000, wherein a slurry phase polymerization process is used in the first reactor system and a gas phase polymerization process is used in the second reactor system, wherein hydrogen is introduced to the first reactor system in an amount up to about 10,000 mppm, based on the total amount of olefins introduced to the first reactor system, wherein hydrogen is introduced to the second reactor system in amount of from about 500 mppm to about 20,000 mppm, based on the total amount of olefins introduced to the second reactor system, and, wherein hydrogen is introduced to the third reactor in an amount of from about 0 mppm to about 10.000 mppm. 22. The process of claim 19, wherein the zinc to titanium molar ratio ranges from about 5 to about 5,000 or from about 10 to about 2,000, wherein a slurry phase polymerization process is used in the first reactor system and a gas phase polymerization process is used in the second reactor system, wherein hydrogen is introduced to the first reactor system in amount of from about 500 mppm to about 20,000 mppm, based on the total amount of olefins introduced to the first reactor system, and wherein hydrogen is introduced to the second reactor system in an amount up to about 10,000 mppm, based on the total amount of olefins introduced to the second reactor system, and wherein hydrogen is introduced to the third reactor system in an amount of from about 0 mppm to about 10.000 mppm. 23. The process of claim 19, wherein the broad or bimodal impact comprises a rubber phase dispersed in a broad or bimodal polypropylene homopolymer crystalline phase or in a broad or bimodal random copolymer polypropylene crystalline phase, wherein an amount of soluble fraction in the impact copolymer ranges from about 5 wt% to about 40 wt%, wherein the at least one other α-olefin comonomer in the crystalline phases is from about 1 wt% to about 10 wt%, the at least one other α-olefin comonomer in the soluble fraction is from about 25 wt% to about 60 wt%, and, wherein the impact copolymer has a melt flow rate of about 30 to about 1,000, as measured by ASTM D1238.

24. A process for melt blowing the homopolymer or copolymer of any claims 2, 7, 10, 15, or 22. 25. A fiber or fabric made from the homopolymer or copolymer of any claims 2, 7, 10, 15, or 22.