Ultra-highly controlled radical polymerization

Abstract

The present invention relates to a method for producing a polymer by radical polymerization, and more particularly to a method for producing a polymer by ultra-highly controlled radical polymerization.

Description

[Technical field]

[0001] The present invention relates to a method for producing a polymer by radical polymerization, and more particularly to a method for producing a polymer by ultra-highly controlled radical polymerization. [Background technology]

[0002] Controlled radical polymerization (CRP) techniques are traditionally utilized for the synthesis of high performance functional materials and functional polymers that exhibit unique properties and can be used for various specialized applications such as adhesives, lubricants, coatings, dispersions and biological applications including drug delivery. Examples of such techniques are atom transfer radical polymerization (ATRP), reversible addition-fragmentation chain transfer (RAFT) and nitroxide mediated polymerization (NMP). In traditional ATRP, NMP and RAFT techniques, polymerization is carried out by adding all the reagents including monomer, initiator, catalyst and chain transfer agent at once. Traditional methods of CRP techniques have many challenges, including (i) the difficulty of introducing relatively air-sensitive polymerization into existing plants built for traditional radical polymerization, and (ii) the possibility of uncontrolled exothermic processes due to the presence of large amounts of monomer in the reactor, especially for highly reactive acrylates.

[0003] Approaches for improving the level of control in these various CRP processes are known in the art. The improvements are directed to the control of the exothermic reaction by controlled supply of the reducing agent. In the state of the art, polymerization processes with an emphasis on improving industrial scalability are known and are described, for example, in the following references:

[0004] US Pat. No. 9,012,528 B2 describes a polymerization process which includes a step of continuously or intermittently feeding a reducing agent or a radical precursor to the reaction medium.

[0005] US Pat. No. 8,822,610 B2 describes a method for operating an ATRP polymerization process, which includes mixing an unsaturated monomer, an atom transfer radical polymerization initiator, a metal catalyst, and optionally a ligand to form a mixture.

[0006] U.S. Pat. No. 5,637,646 B2 describes a process for polymerizing free-radically polymerizable vinyl monomers under adiabatic conditions in a batch reactor, comprising the steps of providing a mixture comprising a free-radically polymerizable vinyl monomer, a free-radical initiator, optionally a chain transfer agent, and a crosslinking agent.

[0007] WO 2009 / 155303 A2 describes a method for conducting controlled radical polymerization comprising providing a mixture of at least one monomer, at least one monomer solvent, at least one metal coordination compound and at least one initiator.

[0008] The methods and compositions disclosed in the prior art have limitations. The traditional ATRP process is not suitable for industrial applications due to shortcomings such as excessive heat generation, the need for an excessive amount of catalyst due to unavoidable radical-radical termination, sensitivity to oxygen that can result in the termination of the polymerization reaction, and uncontrolled exothermic process due to the presence of a large amount of monomer in the reactor. In the methods disclosed in the prior art, the monomer is added to the reaction vessel at once. Adding the monomer at once at the beginning of the polymerization ensures low oxygen introduction during the polymerization process and a more uniform molecular weight distribution. However, when highly reactive monomers such as hydroxyethyl acrylate (HEA) or methyl acrylate are used in the CRP process, either by conventional or continuous reducing agent feeding methods, there always remains a high risk of uncontrolled exotherm. This makes the polymerization difficult to carry out on a large scale. Moreover, in the continuous monomer feeding method utilized in the traditional CRP process, oxygen and inhibitors react with the catalyst and the reaction is terminated. In addition, control over the polymer molecular weight is lost at high monomer conversion due to diffusion-controlled reaction in the traditional CRP process.

[0009] In conventional controlled radical polymerization (CRP) or even advanced controlled radical polymerization, all monomers are added at once, before the addition of other reagents. Generally, these controlled radical polymerization methods are used for monomers with low reactivity and perhaps for small amounts, and the reaction in such a situation does not produce an exotherm on a laboratory scale. However, these methods are not suitable for highly reactive monomers such as HEA or for large-scale reactions, which do produce an exotherm. Conventional methods may also require longer addition times. [Prior art documents] [Patent documents]

[0010] [Patent Document 1] U.S. Patent No. 9,012,528B2 [Patent Document 2] U.S. Patent No. 8,822,610B2 [Patent Document 3] U.S. Patent No. 5,637,646B2 [Patent Document 4] International Publication No. 2009 / 155303A2 Summary of the Invention [Problem to be solved by the invention]

[0011] Thus, there is a need for improved methods for the polymerization of radically polymerizable and highly reactive monomers. Additionally, there is a need for methods that can provide better control over mitigation of exotherms and eliminate the requirement to have large amounts of reactive monomer in the reactor at a given time.

[0012] It is therefore an object of the present invention to provide an improved process for producing polymers with excellent control of exotherm which overcomes the above mentioned drawbacks.It is another object of the present invention to provide an improved controlled radical polymerization process for industrial scale synthesis of polymers.

[0013] Surprisingly, it has been found that the controlled feeding of free radically polymerizable monomers during the production of a polymer provides excellent control of heat generation. Moreover, this method provides not only excellent control of heat generation, but also good control over the molecular weight of the resulting polymer, as reflected in the narrow polydispersity of the polymer or copolymer, and the synthesis of block copolymers obtained by the method of the present invention. [Means for solving the problem]

[0014] Thus, in one aspect, the present invention provides a method for producing a polymer comprising the steps of: i) a) at least one transition metal catalyst; b) at least one reducing agent, and c) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: ii) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, wherein the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii).

[0015] The present invention has at least one of the following advantages: (i) the methods described herein allow for the controlled polymerization of polymerizable monomers; (ii) the methods described herein provide excellent control of exotherm and prevent explosions due to uncontrolled exotherm during polymerization reactions; (iii) the methods described herein, unlike traditional controlled radical polymerization methods, allow for controlled exotherm even upon continuous addition of both oxygen and inhibitor to the reaction mixture; (iv) the methods described herein can be carried out under air-sensitive conditions in existing plant settings; (v) the processes described herein provide good control of the molecular weight of the resulting polymer; (vi) the polymers obtained by the process of the present invention have narrow polydispersities; (vii) the processes described herein can be carried out as semi-batch and continuous processes to suit the requirements of industrial scale production; (viii) the processes described herein are suitable for the polymerization of highly reactive monomers without the risk of uncontrolled exotherm; (ix) the processes described herein can be carried out using low amounts of catalysts and initiators; (x) The methods described herein are safe methods for carrying out the polymerization of highly reactive monomers on a large scale.

[0016] Other objects, advantages and uses of the present invention will become apparent to those skilled in the art from the following detailed description. [Brief description of the drawings]

[0017] [Figure 1] 1 is a graph showing a temperature profile tracking the reaction temperature during the polymerization reaction according to Example 1 (copolymer I). The detected temperature is the recorded temperature of the reaction mixture and the set temperature is the desired temperature of the reaction mixture. Starting point "a" shows the initial setting conditions of feeding raw material 8 (Table 1) to the reaction flask containing 1-7 at a set temperature of 80° C.; "b" shows the addition of raw material 9 (Table 1) after completion of step A to the reaction flask; "c" shows the addition of reducing agent solution 10-11 (Table 1) to the reaction flask; "d" shows the feeding of monomer mixture 12-14 (Table 1) to the reaction flask; "e" shows the change of the set temperature to 90° C. [Diagram 2] 1 is a graph showing experimental GPC chromatography results for Example 1 (Copolymer I). The Mp values ​​for Copolymer I from Table 2 are shown in the figure. [Diagram 3]1 is a graph showing a temperature profile tracking the reaction temperature during the polymerization reaction according to Example 2 (Copolymer II). The detected temperature is the recorded temperature of the reaction mixture and the set temperature is the desired temperature of the reaction mixture. Starting point "a" indicates the initial set conditions of feeding feedstock 8 (Table 3) to the reaction flask containing materials 1-7 (Table 3) at a set temperature of 73° C.; "b" indicates the addition of feedstock 9 (Table 3) after completion of step A to the reaction flask; "c" indicates the addition of reducing agent solution 10-11 (Table 3) to the reaction flask; "d" indicates the feeding of monomer mixture 12-14 (Table 3) to the reaction flask; "e" indicates the change of the set temperature to 80° C.; "f" indicates the change of the set temperature to 90° C. [Figure 4] 1 is a graph showing experimental GPC chromatography results for Example 2 (Copolymer II). The Mp values ​​for Copolymer II from Table 4 are shown in the figure. [Diagram 5] 1 is a graph showing a temperature profile tracking the reaction temperature during a polymerization reaction according to Comparative Example 1 (Copolymer III). The detected temperature is the recorded temperature of the reaction mixture, and the set temperature is the desired temperature of the reaction mixture. Starting point "a" indicates the initial set conditions of feeding Feedstocks 7-8 (Table 5) to the reaction flask containing Feedstocks 1-6 (Table 5); "b" indicates the addition of Feedstocks 9-12 (Table 5) in Step B; "c" indicates the addition of Reducing Agent Solution 13-14 (Table 5) to the reaction flask; "d" indicates the cessation of heating and application of cooling air to control the exotherm; "e" indicates the cessation of the cooling air conditions; "f" indicates the resumption of cooling air; "g" indicates the cessation of the cooling air conditions; "h" indicates the resumption of cooling air; "i" indicates the cessation of the cooling air conditions; "j" indicates the resumption of heating at a set temperature of 80°C. [Figure 6] 1 is a graph showing the experimental GPC chromatography results for Comparative Example 1 (Copolymer III). The Mp values ​​for Copolymer III from Table 6 are shown in the figure. [Figure 7]1 is a graph showing a temperature profile tracking the reaction temperature during a polymerization reaction according to Example 3 (Polymer IV). The detected temperature is the recorded temperature of the reaction mixture, and the set temperature is the desired temperature of the reaction mixture. Starting point "a" indicates the initial set condition of feeding Feedstock 8 (Table 7) to the reaction flask containing Materials 1-7 (Table 7) at a set temperature of 60°C; "b" indicates the complete addition of Feedstock 8 (Table 5); "c" indicates the change of the set temperature to 70°C; "d" indicates the temperature increase due to self-heating, which subsides upon application of cooling air; "e" indicates the change of the set temperature to 67°C; "f" indicates the cessation of the cooling air condition; "g" indicates the change of the set temperature to 60°C; "h" indicates the change of the set temperature to 70°C; "i" indicates the change of the set temperature to 80°C. [Figure 8] 1 is a graph showing experimental GPC chromatography results for Example 3 (Polymer IV). The Mp values ​​for Polymer IV from Table 8 are shown in the figure. [Figure 9] 1 is a graph showing a temperature profile tracking the reaction temperature during the polymerization reaction according to Comparative Example 2 (Polymer V). The detected temperature is the temperature of the reaction mixture and the set temperature is the desired temperature of the reaction mixture. Starting point "a" indicates the initial set conditions of feeding reducing agents 7-8 (Table 9) to the reaction flask containing materials 1-6 (Table 7) at a set temperature of 60° C.; "b" indicates the cessation of heating and application of cold air conditions; "c" indicates the addition of benzothiazine inhibitor (3 wt % relative to the total amount of HEA monomer). [Figure 10]1 is a graph showing a temperature profile tracking the reaction temperature during the polymerization reaction according to Example 4 (copolymer VII). The detected temperature is the recorded temperature of the reaction mixture and the set temperature is the desired temperature of the reaction mixture. Starting point "a" shows the initial setting conditions of feeding monomer 9 (Table 10) to the reaction flask containing monomers 1-8 (Table 10) at a set temperature of 110° C.; "b" and "c" show the increase in set temperature to 115° C. and 120° C., respectively. The end of monomer feed in step A and the increase in set temperature to 125° C. are shown at "d". After a 1 hour hold at 125° C., the temperature was set to 120° C. and mixture "10-11" was added. This is shown at "e". When the temperature reached 120° C., monomer mixture "12-13" was fed at a constant rate. This is shown at "f". [Figure 11] 1 is a graph showing experimental GPC chromatography results for Example 4 (Copolymer VI). The Mp values ​​for Copolymer VI in Table 11 are shown in the figure. [Figure 12] 1 is a graph showing a temperature profile tracking the reaction temperature during the polymerization reaction according to Comparative Example 3 (Polymer VI). The detected temperature is the recorded temperature of the reaction mixture and the set temperature is the desired temperature of the reaction mixture. Starting point "a" shows the initial set conditions of feeding initiator mixture "7-8" (Table 12) to the reaction flask containing "1-6" and "9" (Table 12) at a set temperature of 110°C; "b" shows the quenching of the reaction with inhibitor and cooling air. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0018] The following detailed description is merely exemplary in nature and is not intended to limit the invention or the application and uses of the invention. Moreover, there is no intention to be bound by any theory presented in the preceding technical field, background, brief summary or the following detailed description.

[0019] As used herein, the terms "comprising," "comprise," and "comprised of" are synonymous with "including," "includes," or "containing," "contains," and are inclusive or open-ended and do not exclude additional, unrecited members, elements, or method steps. As used herein, the terms "comprising," "including," and "comprising" include the terms "consisting of," "consists," and "consists of."

[0020] The terms "(a)", "(b)", "(c)", "(d)", etc. and the like in the description and claims are used to distinguish between similar elements and are not necessarily used to describe them in sequential or chronological order. It is to be understood that the terms so used are interchangeable under appropriate circumstances and that the embodiments of the subject matter described herein may operate in other sequences than those described or illustrated herein. When the terms "(A)", "(B)", and "(C)", or "(a)", "(b)", "(c)", "(d)", "(i)", "(ii)", etc. refer to steps of a method or use or assay, there is no consistency in the time or time interval between the steps, i.e., the steps may be performed simultaneously or there may be a time interval of seconds, minutes, hours, days, weeks, months or even years between such steps, unless otherwise indicated in this application, as set forth herein above or below.

[0021] In the following passages, various aspects of the subject matter are defined in more detail. Each aspect thus defined may be combined with any other aspect, unless clearly indicated to the contrary. In particular, any feature indicated as being preferred or advantageous may be combined with any other feature indicated as being preferred or advantageous.

[0022] References throughout this specification to "one embodiment" or "embodiment" mean that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment of the present invention. Thus, the appearances of the phrases "in one embodiment" or "in an embodiment" in various places throughout this specification may, but do not necessarily, all refer to the same embodiment. Furthermore, in one or more embodiments, features, structures, or characteristics may be combined in any suitable manner, as would be apparent to one of ordinary skill in the art from this disclosure. Furthermore, as would be understood by one of ordinary skill in the art, some embodiments described herein include some features but not other features included in other embodiments, and combinations of features of different embodiments are intended to be within the scope of the subject matter and form various embodiments. For example, in the appended claims, any of the claimed embodiments may be used in any combination.

[0023] Furthermore, ranges defined throughout this specification are inclusive of the endpoints as well, i.e., a range of 1 to 10 means that both 1 and 10 are included in the range. For the avoidance of doubt, Applicant reserves the right to any equivalents pursuant to applicable law.

[0024] For purposes of this invention, a block polymer or block copolymer is defined as a polymer or copolymer formed when two or more monomers are clustered together to form a "block" of repeating units.

[0025] Reference to the term "copolymer" throughout this specification is meant to include block or random copolymers obtained by radical polymerization.

[0026] For purposes of this invention, a controlled or living polymerization process (CRP) is defined as a process in which chain transfer and termination reactions are essentially absent in relation to the polymer propagation process.

[0027] For purposes of this invention, the ATRP process is defined as a polymerization method to provide highly uniform products with controlled architecture, also referred to as controlled radical polymerization (CRP).

[0028] For purposes of this invention, very high controlled radical polymerization or very high ATRP is a polymerization process carried out under monomer starvation conditions.

[0029] For purposes of this invention, monomer starvation is defined as a condition in a polymerization process where monomer is metered in and the monomer is not added all at once at the start of the reaction.

[0030] For purposes of the present invention, the term "monomer residue" is the residue of a monomer resulting from polymerization of the corresponding unsaturated monomer.

[0031] For purposes of this invention, an atom transfer radical polymerization initiator is defined as a molecule that contains one or more transferable atoms or groups and can be considered a contributor to the number of growing polymer chains during polymerization.

[0032] For purposes of this invention, a reducing agent is defined as an agent capable of donating one or more electrons to reduce an inactive metal catalyst to produce an active metal catalyst.

[0033] For purposes of the present invention, polydispersity or polydispersity index (PDI) is defined as a measure of the molecular weight distribution of a given polymer.

[0034] For the purposes of the present invention, the weight average molecular weight (M w ), number average molecular weight (M n ) and maximum peak molecular weight (M p ) is determined by gel permeation chromatography at 40° C. using a high performance liquid chromatography pump and a refractive index detector. The eluent is tetrahydrofuran with an elution rate of 1 ml / min. Calibration is performed with polystyrene standards.

[0035] For purposes of the present invention, "mass %" or "wt%" as used herein is based on the total weight of the coating composition. Further, as described below, the sum of the wt% of all compounds in each component equals 100 wt%.

[0036] The above mentioned measurement techniques are well known to those skilled in the art and therefore are not intended to be limitations of the present invention.

[0037] For the purposes of the present invention, the simple ATRP method with components such as metal catalyst, reducing agent, initiator and monomer for the preparation of polymers or copolymers can be referred to in the following patents and patent applications: US Patent No. 5,763,546, US Patent No. 6,121,371, US Patent No. 7,019,082, US Patent Application No. 2009 / 534,827, US Patent No. 6,365,666 and US Patent No. 6,642,301, PCT / US2006 / 048656 and US Patent Application Publication No. 2011 / 0082230. ATRP is considered to be a preferred method for the controlled / living polymerization of radical copolymerizable monomers. The general mechanism and detailed description of polymerization by ATRP method can be referred to in US Patent No. 8,822,610.

[0038] Conventional ATRP methods often require high catalyst concentrations of about 0.1M in the polymerization reaction of bulk monomers. High levels of catalyst used in the initial ATRP reaction were required to overcome the effects of the inevitable rise in the concentration of high oxidation state catalyst due to the inevitable radical-radical termination reaction. Special handling procedures are also required to remove all oxygen and oxides from the system before the addition of the catalyst, which can be rapidly oxidized. The energy used in these purification methods and / or the need for deoxygenated systems contribute to the generation of chemical waste and additional costs. These are the main factors that limit the commercial application of ATRP. In recent advances, efforts have been made to reduce the concentration of catalyst used by adding reducing agents or initiators to continuously regenerate low oxidation state activators with the accumulation of high oxidation state activators, as described in WO 2007 / 075817. However, this approach has several drawbacks, such as the requirement to maintain a slow reaction of highly active monomers, the need for precise temperature control, and a highly exothermic reaction. Methods to overcome these limitations, especially on a large scale, are disclosed below.

[0039] The present invention fulfills the need in the art for a controlled radical polymerization method that can reliably produce controlled polymer products with desirable properties through ultra-highly controlled radical polymerization. The polymers obtained by the methods described herein have excellent control of exotherm, good control over molecular weight and narrow polydispersity. The controlled polymer products obtained by the methods described herein have numerous applications, such as coatings, detergents and surfactants, paints, pigments, adhesives, lubricants and biological applications. Furthermore, the methods described herein can be practiced on a small, large or commercial scale.

[0040] Accordingly, an aspect of the present invention is a method for producing a polymer comprising at least i) a) at least one transition metal catalyst; b) at least one reducing agent, and c) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: ii) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii).

[0041] The rate of addition of the at least one free radically copolymerizable monomer in step (ii) in the range of 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically copolymerizable monomer, may be constant or may vary within the ranges stated within the total time of monomer addition.

[0042] In an embodiment of the invention, (a) the at least one transition metal catalyst is a transition metal halide catalyst.

[0043] In a preferred embodiment of the invention, the metal halide catalyst is itself inert to the production of radicals.

[0044] In another preferred embodiment of the present invention, the metal halide catalyst is active.

[0045] In a preferred embodiment of the present invention, the transition metal halide catalyst is selected from the group consisting of iron chloride, iron bromide, iron iodide, ruthenium chloride, ruthenium bromide, ruthenium iodide, copper chloride, copper bromide and copper iodide. In a more preferred embodiment of the present invention, the transition metal halide catalyst is selected from the group consisting of copper chloride, copper bromide and copper iodide.

[0046] In another preferred embodiment of the present invention, the (a) at least one transition metal catalyst is added in an amount ranging from 0.1 ppm to 250 ppm. In a more preferred embodiment of the present invention, the (a) at least one transition metal catalyst is added in an amount ranging from 1 ppm to 200 ppm. In a most preferred embodiment of the present invention, the (a) at least one transition metal catalyst is added in an amount ranging from 1 ppm to 150 ppm. In a particularly most preferred embodiment of the present invention, the (a) at least one transition metal catalyst is added in an amount ranging from 5 ppm to 100 ppm.

[0047] In another embodiment of the invention, (b) the at least one reducing agent is selected from the group consisting of stannous 2-ethylhexanoate, sulfites, bisulfites, thiosulfites, mercaptans, hydroxylamines, amines, hydrazine, phenylhydrazine, hydrazones, hydroquinones, food preservatives, flavonoids, beta-carotene, vitamin A, C-tocopherol, vitamin E, propyl gallate, octyl gallate, propionic acid, ascorbic acid, sorbates, reducing sugars, sugars containing aldehyde groups, glucose, lactose, fructose, dextrose, potassium tartrate, nitrites, dextrins, aldehydes, glycine, and antioxidants.

[0048] In yet another embodiment of the present invention, (b) the at least one reducing agent is a free radical initiator.

[0049] In a preferred embodiment of the invention, the free radical initiator is selected from the group consisting of ammonium persulfate, hydrogen peroxide, acetyl peroxide, cumyl peroxide, tert-butyl peroxide, propionyl peroxide, benzoyl peroxide, chlorobenzoyl peroxide, dichlorobenzoyl peroxide, bromomethylbenzoyl peroxide, lauroyl peroxide, sodium persulfate, potassium persulfate, diisopropyl peroxycarbonate, tetralin hydroperoxide, 1-phenyl-2-methylpropyl-1-hydroperoxide, tert-butyl peroxytriphenylacetate hydroperoxide, tert-butyl performate, and tert-butyl peroxytriphenylacetate. t-Butyl, tert-butyl peracetate, tert-butyl perbenzoate, tert-butyl perphenylacetate, tert-butyl permethoxyacetate, tert-butyl per-N-(3-tolyl)carbamate, 2,2'-azobispropane, 2,2'-dichloro-2,2'-azobispropane, 1,1'-azo(methylethyl)diacetate, 2,2'-azobis(2-amidinopropane)hydrochloride, 2,2'-azobis(2-amidinopropane)nitrate, 2,2'-azobisisobutane, 2,2'-azobisisobutyramide, 2,2'-azobisisobutyronitrile, Methyl 2,2'-azobis-2-methylpropionate, 2,2'-dichloro-2,2'-azobisbutane, 2,2'-azobis-2-methylbutyronitrile, 2,2'-azobis-2-methylpropionitrile, ethyl 2-bromoisobutyrate, dimethyl 2,2'-azobisisobutyrate, sodium 1,1'-azobis(1-methylbutyronitrile-3-sulfonate), 2-(4-methylphenylazo)-2-methylmalonodinitrile, 4,4'-azobis-4-cyanovaleric acid, 3,5-dihydroxymethylphenylazo-2-methylmalonodinitrile, 2-(4 -Bromophenylazo)-2-allylmalonodinitrile, 2,2'-azobis-2-methylvaleronitrile, 4,4'-azobis-4-cyanodimethylvalerate, 2,2'-azobis-2,4-dimethylvaleronitrile, 2,2'-azobis-4-methoxy-2,4-dimethylvaleronitrile, 1,1'-azobiscyclohexanenitrile, 2,2'-azobis-2-propylbutyronitrile, 1,1'-azobis-chlorophenylethane, 1,1'-azobis-1-cyclohexanecarbonitrile, 1,1'-azobis-1-cycloheptanenitrile, 1,The compound is selected from the group consisting of 1'-azobis-1-phenylethane, 1,1'-azobiscumene, 4-nitrophenylazobenzyl ethyl cyanoacetate, phenylazodiphenylmethane, phenylazotriphenylmethane, 4-nitrophenylazotriphenylmethane, 1'-azobis-1,2-diphenylethane, poly(4,4'-azobis-4-cyano bisphenol) , poly(2,2'-azobisisobutyric acid tetraethylene glycol) , 1,4-bis(pentaethylene)-2-tetrazene, 1,4-dimethoxycarbonyl-1,4-diphenyl-1-2-tetrazene, and mixtures thereof.

[0050] In a more preferred embodiment of the present invention, the free radical initiator is 2,2'-azobispropane, 2,2'-dichloro-2,2'-azobispropane, 1,1'-azo(methylethyl)diacetate, 2,2'-azobis(2-amidinopropane)hydrochloride, 2,2'-azobis(2-amidinopropane)nitrate, 2,2'-azobisisobutane, 2,2'-azobisisobutyramide, 2,2'-azobisisobutyronitrile, 2,2'-azobis-2-methylmethylpropionate, 2,2'-dichloro-2,2'-azobis ...isobutane, 2,2'-azobisisobutyramide, 2,2'-azobisisobutyronitrile, 2,2'-azobis-2-methylmethylpropionate, 2, ,2'-Azobis-2-methylbutyronitrile, 2,2'-Azobis-2-methylpropionitrile, Ethyl 2-bromoisobutyrate, Dimethyl 2,2'-Azobisisobutyrate, Sodium 1,1'-Azobis(1-methylbutyronitrile-3-sulfonate), 2-(4-methylphenylazo)-2-methylmalonodinitrile, 4,4'-Azobis-4-cyanovaleric acid, 3,5-dihydroxymethylphenylazo-2-methylmalonodinitrile, 2-(4-bromophenylazo)-2-allylmalonodinitrile, 2,2'-Azobis-2-methyl Cylvaleronitrile, 4,4'-azobis-4-cyanodimethylvalerate, 2,2'-azobis-2,4-dimethylvaleronitrile, 2,2'-azobis-4-methoxy-2,4-dimethylvaleronitrile, 1,1'-azobiscyclohexanenitrile, 2,2'-azobis-2-propylbutyronitrile, 1,1'-azobis-chlorophenylethane, 1,1'-azobis-1-cyclohexanecarbonitrile, 1,1'-azobis-1-cycloheptanenitrile, 1,1'-azobis-1-phenylethane, 1,1'-azobisqume phenylazobenzyl ethyl cyanoacetate, phenylazodiphenylmethane, phenylazotriphenylmethane, 4-nitrophenylazotriphenylmethane, 1'-azobis-1,2-diphenylethane, poly(bisphenol 4,4'-azobis-4-cyanopentanoate), poly(tetraethylene glycol 2,2'-azobisisobutyrate), 1,4-bis(pentaethylene)-2-tetrazene, 1,4-dimethoxycarbonyl-1,4-diphenyl-1-2-tetrazene, and mixtures thereof.

[0051] In the most preferred embodiment of the invention, the free radical initiator is selected from the group consisting of 2'-azobisisobutyramide, 2,2'-azobisisobutyronitrile, methyl 2,2'-azobis-2-methylpropionate, 2,2'-dichloro-2,2'-azobisbutane, 2,2'-azobis-2-methylbutyronitrile, 2,2'-azobis-2-methylpropionitrile, ethyl 2-bromoisobutyrate, dimethyl 2,2'-azobisisobutyrate and sodium 1,1'-azobis(1-methylbutyronitrile-3-sulfonate).

[0052] In another preferred embodiment of the present invention, the (b) at least one reducing agent is added in an amount ranging from 100 ppm to 1000,000 ppm. In a more preferred embodiment of the present invention, the (b) at least one reducing agent is added in an amount ranging from 100 ppm to 100,000 ppm. In a most preferred embodiment of the present invention, the (b) at least one reducing agent is added in an amount ranging from 100 ppm to 50,000 ppm. In a particularly most preferred embodiment of the present invention, the (b) at least one reducing agent is added in an amount ranging from 1000 ppm to 50,000 ppm, in each case relative to the total amount of the final polymer mass.

[0053] In another embodiment of the present invention, c) the at least one atom transfer radical polymerization initiator is selected from the group consisting of sulfonyl halides, alkyl halides, and substituted alkyl halides.

[0054] In a preferred embodiment of the present invention, the alkyl halide and substituted alkyl halide are selected from the group consisting of benzyl bromide, benzyl chloride, ethyl bromoacetate, diethyl 2-bromo-2-methylmalonate, ethyl 2-bromoisobutyrate, methyl 2-bromopropionate, ethyl 2-chloroisobutyrate, and 1,2-bis(2-bromoisobutyryloxy)ethane, toluenesulfonyl chloride. In a more preferred embodiment of the present invention, the alkyl halide and substituted alkyl halide are selected from the group consisting of diethyl 2-bromo-2-methylmalonate, ethyl 2-bromoisobutyrate, methyl 2-bromopropionate, ethyl 2-chloroisobutyrate, and 1,2-bis(2-bromoisobutyryloxy)ethane, toluenesulfonyl chloride.

[0055] In another preferred embodiment of the present invention, (c) the at least one atom transfer radical polymerization initiator is added in an amount ranging from 1 ppm to 500,000 ppm. In a more preferred embodiment of the present invention, (c) the at least one atom transfer radical polymerization initiator is added in an amount ranging from 10 ppm to 500,000 ppm. In a most preferred embodiment of the present invention, (c) the at least one atom transfer radical polymerization initiator is added in an amount ranging from 100 ppm to 500,000 ppm. In a particularly most preferred embodiment of the present invention, (c) the at least one atom transfer radical polymerization initiator is added in an amount ranging from 1000 ppm to 500,000 ppm, in each case relative to the total final polymer mass.

[0056] In a preferred embodiment of the invention, the at least one free-radically copolymerizable monomer is an ethylenically unsaturated monomer.

[0057] In a preferred embodiment of the present invention, at least one free-radically polymerizable monomer is hydrophobic. In another preferred embodiment of the present invention, at least one free-radically polymerizable monomer is hydrophilic.

[0058] In another preferred embodiment of the present invention, the ethylenically unsaturated monomer is selected from the group consisting of styrene, α-methylstyrene, methyl acrylate, ethyl acrylate, butyl acrylate, isobutyl acrylate, dodecyl acrylate, n-octyl acrylate, 2-chloroethyl acrylate, carboxyethyl acrylate, phenyl acrylate, benzyl acrylate, α-chloromethyl acrylate, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacrylate, dodecyl methacrylate, n-octyl methacrylate, methacryloyl acrylate, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacrylate, dodecyl methacrylate, n-octyl methacrylate, methyl ... 2-Chloroethyl acrylate, carboxyethyl methacrylate, phenyl methacrylate, α-chloromethyl methacrylate, benzyl methacrylate, butadiene, isoprene, methacrylonitrile, acrylonitrile, vinyl methyl ether, vinyl isobutyl ether, vinyl ethyl ether, vinyl acetate, vinyl propionate, vinyl benzoate, vinyl butyrate, vinyl methyl ketone, vinyl hexyl ketone, methyl isopropenyl ketone, vinylidene chloride, chlorovinylidene fluoride, N-vinylpyrrolidone, N-vinylcarbazole, acrylonitrile, vinyl methyl ether, vinyl isobutyl ether, vinyl ethyl ether, vinyl acetate, vinyl propionate, vinyl benzoate, vinyl butyrate, vinyl methyl ketone, vinyl hexyl ketone, methyl isopropenyl ketone, vinylidene chloride, vinylidene chlorofluoride, N-vinylpyrrolidone, N-vinylcarbazole, acrylonitrile, vinyl methyl ether, vinyl hexyl ketone ... acrylic acid, methacrylic acid, acrylamide, methacrylamide, vinylpyridine, vinylpyrrolidone, vinyl-N-methylpyridinium chloride, vinylnaphthalene, p-chlorostyrene, vinyl chloride, vinyl bromide, vinyl fluoride, ethylene, propylene, butylene, isobutylene, 2-ethylbutyl acrylate, 2-ethylbutyl methacrylate, 2-ethylhexyl acrylate, 2-ethylhexyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl acrylate, methacrylic acid Selected from the group consisting of 2-hydroxypropyl, 3-hydroxypropyl acrylate, 3-hydroxypropyl methacrylate, 3-hydroxybutyl acrylate, 3-hydroxybutyl methacrylate, 4-hydroxybutyl acrylate, 4-hydroxybutyl methacrylate, 6-hydroxyhexyl acrylate, 6-hydroxyhexyl methacrylate, 3-hydroxy-2-ethylhexyl acrylate, 3-hydroxy-2-ethylhexyl methacrylate, glycidyl acrylate, glycidyl methacrylate and mixtures thereof.

[0059] In yet another preferred embodiment of the present invention, the ethylenically unsaturated monomer is selected from the group consisting of styrene, α-methylstyrene, methyl acrylate, ethyl acrylate, butyl acrylate, isobutyl acrylate, dodecyl acrylate, n-octyl acrylate, 2-chloroethyl acrylate, carboxyethyl acrylate, phenyl acrylate, benzyl acrylate, α-chloromethyl acrylate, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacrylate, dodecyl methacrylate, n-octyl methacrylate, 2-chloroethyl methacrylate, carboxyethyl methacrylate, phenyl methacrylate, α-chloromethyl methacrylate, benzyl methacrylate, methacrylonitrile, acrylonitrile, N-vinylpyrrolidone, N-vinylcarbazole, acrylic acid, methacrylic acid, acrylamide, methacrylamide, vinylpyridine, vinylpyrrolidone, Selected from the group consisting of vinyl-N-methylpyridinium chloride, vinyl naphthalene, vinyl fluoride, ethylene, 2-ethylbutyl acrylate, 2-ethylbutyl methacrylate, 2-ethylhexyl acrylate, 2-ethylhexyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl acrylate, 2-hydroxypropyl methacrylate, 3-hydroxypropyl acrylate, 3-hydroxypropyl methacrylate, 3-hydroxybutyl acrylate, 3-hydroxybutyl methacrylate, 4-hydroxybutyl acrylate, 4-hydroxybutyl methacrylate, 6-hydroxyhexyl acrylate, 6-hydroxyhexyl methacrylate, 3-hydroxy-2-ethylhexyl acrylate, 3-hydroxy-2-ethylhexyl methacrylate, glycidyl acrylate, glycidyl methacrylate and mixtures thereof.

[0060] In yet another preferred embodiment of the present invention, the ethylenically unsaturated monomer is selected from the group consisting of styrene, α-methylstyrene, methyl acrylate, ethyl acrylate, butyl acrylate, isobutyl acrylate, dodecyl acrylate, n-octyl acrylate, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacrylate, dodecyl methacrylate, n-octyl methacrylate, phenyl methacrylate, α-chloromethyl methacrylate, benzyl methacrylate, methacrylonitrile, acrylonitrile, N-vinylpyrrolidone, N-vinylcarbazole, acrylic acid, methacrylic acid, acrylamide, methacrylic amine ...methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacrylate, dodecyl methacrylate, n-octyl methacrylate, phenyl methacrylate, methyl α-chloromethacrylate, benzyl methacrylate, methacrylonitrile, methyl methacrylate, methyl methacrylate, methyl methacrylate, The vinyl acrylate or vinyl methacrylate may be selected from the group consisting of dimethyl acrylate, dimethyl acrylate, dimethyl meth ...

[0061] In yet another preferred embodiment of the present invention, the ethylenically unsaturated monomer is selected from the group consisting of styrene, butyl acrylate, methyl methacrylate, butyl methacrylate, 2-ethylhexyl acrylate, 2-ethylhexyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl acrylate, 2-hydroxypropyl methacrylate, 3-hydroxypropyl acrylate, 3-hydroxypropyl methacrylate, glycidyl methacrylate and mixtures thereof.

[0062] In an embodiment of the present invention, the at least one free-radically copolymerizable monomer is added intermittently or continuously.

[0063] In a preferred embodiment of the invention, the at least one free radically polymerizable monomer is added at a rate ranging from 0.17 to 0.83 wt% / min, based on the total weight of the at least one free radically polymerizable monomer. In a more preferred embodiment of the invention, the at least one free radically polymerizable monomer is added at a rate ranging from 0.25 to 0.50 wt% / min, based on the total weight of the at least one free radically polymerizable monomer. In either case, the addition rate of the at least one free radically polymerizable monomer may be constant or may vary within the stated ranges within the total time of monomer addition.

[0064] In an embodiment of the invention, the molar ratio of the at least one free radically polymerizable monomer to the at least one transition metal catalyst is in the range of 10:1.0 to 500,000:1.0. In a preferred embodiment of the invention, the molar ratio of the at least one free radically polymerizable monomer to the at least one transition metal catalyst is in the range of 100:1.0 to 250,000:1.0. In a more preferred embodiment of the invention, the molar ratio of the at least one free radically polymerizable monomer to the at least one transition metal catalyst is in the range of 100:1 to 100,000:1.

[0065] In an embodiment of the present invention, the molar ratio of the at least one free radical copolymerizable monomer to the at least one atom transfer radical polymerization initiator is in the range of 1.0:1.0 to 10,000:1.0. In a preferred embodiment of the present invention, the molar ratio of the at least one free radical copolymerizable monomer to the at least one atom transfer radical polymerization initiator is in the range of 2.0:1.0 to 1,000:1.0. In a more preferred embodiment of the present invention, the molar ratio of the at least one free radical copolymerizable monomer to the at least one atom transfer radical polymerization initiator is in the range of 2.0:1.0 to 500:1.0.

[0066] In an embodiment of the present invention, the molar ratio of the at least one transition metal catalyst to the at least one atom transfer radical polymerization initiator is in the range of 0.0005:1.0 to 50:1.0. In a preferred embodiment of the present invention, the molar ratio of the at least one transition metal catalyst to the at least one atom transfer radical polymerization initiator is in the range of 0.0005:1.0 to 5:1.0. In a more preferred embodiment of the present invention, the molar ratio of the at least one transition metal catalyst to the at least one atom transfer radical polymerization initiator is in the range of 0.0005:1.0 to 0.5:1.0.

[0067] In an embodiment of the present invention, the molar ratio of the at least one free radical initiator to the at least one atom transfer radical polymerization initiator added is in the range of 0.005:1.0 to 50:1.0. In a preferred embodiment of the present invention, the molar ratio of the at least one free radical initiator to the at least one atom transfer radical polymerization initiator is in the range of 0.005:1.0 to 5.0:1.0. In a more preferred embodiment of the present invention, the molar ratio of the at least one free radical initiator to the at least one atom transfer radical polymerization initiator is in the range of 0.005:1 to 1:1.

[0068] In an embodiment of the present invention, the polymerization mixture further comprises at least one solvent. In a preferred embodiment of the present invention, the at least one solvent is selected from the group consisting of methanol, ethanol, n-propanol, isopropanol, butanol, butoxyethanol, acetone, butanone, pentanone, hexanone, methyl ethyl ketone, methyl isobutyl ketone, ethyl acetate, butyl acetate, amyl acetate, methoxypropyl acetate, tetrahydrofuran, diethyl ether, ethylene glycol, polyethylene glycol, and mixtures thereof.

[0069] For the purposes of the present invention, suitable ligands may be used in the polymerization reaction for the formation of polymers or copolymers. The ligands may form complexes with the transition metal catalyst during polymerization step (ii). The ligands drive the polymerization reaction in a manner that may aid in the molecular level mixing of the various components in step (i). Representative examples of ligands include, but are not limited to, tris(2-pyridylmethyl)amine (TPMA), tris[2-(dimethylamino)ethyl]amine, N,N,N',N'',N''-pentamethyldiethyltriamine, N,N,N',N'',N'''',N''''-hexamethyltriethylenetetramine, 4,4'-dinonylbipyridine and bipyridine.

[0070] In a preferred embodiment of the present invention, the polymerization of at least one free-radically copolymerizable monomer into a polymer is carried out as a two-phase polymerization process, an emulsion polymerization process, a miniemulsion polymerization process, a microemulsion polymerization process, an inverse emulsion polymerization process or a suspension polymerization process.

[0071] In yet another preferred embodiment of the present invention, the polymerization of at least one free radically polymerizable monomer into a polymer allows for a conversion of at least 90% of the total amount of free radically polymerizable monomers. In a more preferred embodiment of the present invention, the polymerization of at least one free radically polymerizable monomer into a polymer allows for a conversion of at least 95% of the total amount of free radically polymerizable monomers. In a most preferred embodiment of the present invention, the polymerization of at least one free radically polymerizable monomer into a polymer allows for a conversion of at least 99% of the total amount of free radically polymerizable monomers.

[0072] In another embodiment of the invention, the temperature of the polymerization step is maintained in the range of 35° C. to 150° C. In a preferred embodiment of the invention, the temperature of the polymerization step is maintained in the range of 40° C. to 110° C.

[0073] In an embodiment of the present invention, the degree of temperature variation from the target temperature during the monomer addition step (ii) is in the range of ≧−10.0% to ≦+10.0%. In a preferred embodiment of the present invention, the degree of temperature variation from the target temperature during the polymerization step (ii) is in the range of ≧−5.0% to ≦+5.0%.

[0074] In a preferred embodiment of the present invention, the polymerization step is carried out within a time period ranging from 1 hour to 25 hours, inclusive. In a more preferred embodiment of the present invention, the polymerization step is carried out within a time period ranging from 2 hours to 15 hours, inclusive.

[0075] In an embodiment of the present invention, a method for preparing a diblock polymer of formula AB comprises at least (a) subjecting a first reaction mixture comprising at least one free-radically copolymerizable monomer to very high controlled radical polymerization or very high ATRP to form a first polymer block A; (b) subjecting a second reaction mixture comprising at least one free-radically copolymerizable monomer to very high controlled radical polymerization or very high ATRP to form a second polymer block B; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (a) or step (b); The at least one free-radically copolymerizable monomer in step (a) and step (b) may be the same or different.

[0076] The rate of addition of the at least one free radically copolymerizable monomer in the range of 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically copolymerizable monomer in step (a) or step (b), may be constant or may vary within the ranges stated within the total time of monomer addition.

[0077] In another embodiment of the present invention, the first reaction mixture of step (a) comprises at least one transition metal catalyst, at least one reducing agent, at least one atom transfer radical polymerization initiator, and at least one free-radically copolymerizable monomer.

[0078] In another embodiment of the invention, the second reaction mixture of step (b) comprises at least one transition metal catalyst, at least one reducing agent, at least one atom transfer radical polymerization initiator and at least one free radical copolymerizable monomer. The selection of the components of the first and second reaction mixtures and their amounts are according to other embodiments described herein.

[0079] In a preferred embodiment of the present invention, the method for producing a polymer comprises at least i) a) at least one transition metal catalyst; b) at least one reducing agent, and c) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: ii) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii); The degree of temperature change from the target temperature during step (ii) is in the range of -10.0% to +10.0%.

[0080] In another preferred embodiment of the present invention, the method for producing a polymer comprises at least iii) d) at least one transition metal catalyst; e) at least one reducing agent, and f) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: iv) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii); the degree of temperature change from the target temperature during step (ii) is in the range of -10.0% or more and +10.0% or less; The at least one free radically copolymerizable monomer is an ethylenically unsaturated monomer and is selected from the group consisting of styrene, α-methylstyrene, methyl acrylate, ethyl acrylate, butyl acrylate, isobutyl acrylate, dodecyl acrylate, n-octyl acrylate, 2-chloroethyl acrylate, carboxyethyl acrylate, phenyl acrylate, benzyl acrylate, α-chloromethyl acrylate, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacrylate, dodecyl methacrylate, n-octyl methacrylate, and the like. , 2-chloroethyl methacrylate, carboxyethyl methacrylate, phenyl methacrylate, α-chloromethyl methacrylate, benzyl methacrylate, butadiene, isoprene, methacrylonitrile, acrylonitrile, vinyl methyl ether, vinyl isobutyl ether, vinyl ethyl ether, vinyl acetate, vinyl propionate, vinyl benzoate, vinyl butyrate, vinyl methyl ketone, vinyl hexyl ketone, methyl isopropenyl ketone, vinylidene chloride, chlorovinylidene fluoride, N-vinylpyrrolidone, N-vinylcarbazole , acrylic acid, methacrylic acid, acrylamide, methacrylamide, vinylpyridine, vinylpyrrolidone, vinyl-N-methylpyridinium chloride, vinylnaphthalene, p-chlorostyrene, vinyl chloride, vinyl bromide, vinyl fluoride, ethylene, propylene, butylene, isobutylene, 2-ethylbutyl acrylate, 2-ethylbutyl methacrylate, 2-ethylhexyl acrylate, 2-ethylhexyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl acrylate, methacryloyl ... In one embodiment, the acrylate or methacrylate is selected from the group consisting of 2-hydroxypropyl acrylate, 3-hydroxypropyl acrylate, 3-hydroxypropyl methacrylate, 3-hydroxybutyl acrylate, 3-hydroxybutyl methacrylate, 4-hydroxybutyl acrylate, 4-hydroxybutyl methacrylate, 6-hydroxyhexyl acrylate, 6-hydroxyhexyl methacrylate, 3-hydroxy-2-ethylhexyl acrylate, 3-hydroxy-2-ethylhexyl methacrylate, glycidyl acrylate, glycidyl methacrylate, and mixtures thereof.

[0081] In yet another preferred embodiment of the present invention, the method for producing a polymer comprises at least v) g) at least one transition metal catalyst; h) at least one reducing agent, and i) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: vi) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii); the degree of temperature change from the target temperature during step (ii) is in the range of -10.0% or more and +10.0% or less; The at least one free radically copolymerizable monomer is an ethylenically unsaturated monomer, and is selected from the group consisting of styrene, α-methylstyrene, methyl acrylate, ethyl acrylate, butyl acrylate, isobutyl acrylate, dodecyl acrylate, n-octyl acrylate, 2-chloroethyl acrylate, carboxyethyl acrylate, phenyl acrylate, benzyl acrylate, α-chloromethyl acrylate, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacrylate, dodecyl methacrylate, n-octyl methacrylate, 2-chloroethyl methacrylate, carboxyethyl methacrylate, phenyl methacrylate, α-chloromethyl methacrylate, benzyl methacrylate, methacrylonitrile, acrylonitrile, N-vinylpyrrolidone, N-vinylcarbazole, acrylic acid, methacrylic acid, acrylamide, methacrylamide, vinylpyridine, vinylpyrrolide. and mixtures thereof.

[0082] In another preferred embodiment of the present invention, the method for producing a polymer comprises at least vii) j) at least one transition metal catalyst; k) at least one reducing agent, and l) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: viii) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii); the degree of temperature change from the target temperature during step (ii) is in the range of -10.0% or more and +10.0% or less; The at least one free radically copolymerizable monomer is an ethylenically unsaturated monomer, and may be selected from the group consisting of styrene, α-methylstyrene, methyl acrylate, ethyl acrylate, butyl acrylate, isobutyl acrylate, dodecyl acrylate, n-octyl acrylate, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacrylate, dodecyl methacrylate, n-octyl methacrylate, phenyl methacrylate, α-chloromethyl methacrylate, benzyl methacrylate, methacrylonitrile, acrylonitrile, N-vinylpyrrolidone, N-vinylcarbazole, acrylic acid, methacrylic acid, acrylamide, methacrylic acid, amide, vinylpyridine, vinylpyrrolidone, vinylnaphthalene, vinyl fluoride, ethylene, 2-ethylhexyl acrylate, 2-ethylhexyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl acrylate, 2-hydroxypropyl methacrylate, 3-hydroxypropyl acrylate, 3-hydroxypropyl methacrylate, 3-hydroxybutyl acrylate, 3-hydroxybutyl methacrylate, 4-hydroxybutyl acrylate, 4-hydroxybutyl methacrylate, glycidyl acrylate, glycidyl methacrylate and mixtures thereof.

[0083] In another preferred embodiment of the present invention, the method for producing a polymer comprises at least ix) m) at least one transition metal catalyst; n) at least one reducing agent, and o) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: x) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii); the degree of temperature change from the target temperature during step (ii) is in the range of -10.0% or more and +10.0% or less; The at least one free radically copolymerizable monomer is an ethylenically unsaturated monomer selected from the group consisting of styrene, butyl acrylate, methyl methacrylate, butyl methacrylate, 2-ethylhexyl acrylate, 2-ethylhexyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl acrylate, 2-hydroxypropyl methacrylate, 3-hydroxypropyl acrylate, 3-hydroxypropyl methacrylate, glycidyl methacrylate, and mixtures thereof.

[0084] In another preferred embodiment of the present invention, the method for producing a polymer comprises at least i) a) at least one transition metal catalyst; b) at least one reducing agent, and c) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: ii) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii); The degree of temperature change from the target temperature during step (ii) is in the range of -5.0% to +5.0%.

[0085] In yet another preferred embodiment of the present invention, the method for producing a polymer comprises at least iii) d) at least one transition metal catalyst; e) at least one reducing agent, and f) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: iv) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii); The degree of temperature change from the target temperature during step (ii) is in the range of −5.0% or more and +5.0% or less; The at least one free radically copolymerizable monomer is an ethylenically unsaturated monomer, and is selected from the group consisting of styrene, α-methylstyrene, methyl acrylate, ethyl acrylate, butyl acrylate, isobutyl acrylate, dodecyl acrylate, n-octyl acrylate, 2-chloroethyl acrylate, carboxyethyl acrylate, phenyl acrylate, benzyl acrylate, α-chloromethyl acrylate, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacrylate, dodecyl methacrylate, n-octyl methacrylate, 2-chloroethyl methacrylate, carboxyethyl methacrylate, phenyl methacrylate, α-chloromethyl methacrylate, benzyl methacrylate, methacrylonitrile, acrylonitrile, N-vinylpyrrolidone, N-vinylcarbazole, acrylic acid, methacrylic acid, acrylamide, methacrylamide, vinylpyridine, vinylpyrrolide. and mixtures thereof.

[0086] In yet another preferred embodiment of the present invention, the method for producing a polymer comprises at least v) g) at least one transition metal catalyst; h) at least one reducing agent, and i) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: vi) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii); The degree of temperature change from the target temperature during step (ii) is in the range of −5.0% or more and +5.0% or less; The at least one free radically copolymerizable monomer is an ethylenically unsaturated monomer, and may be selected from the group consisting of styrene, α-methylstyrene, methyl acrylate, ethyl acrylate, butyl acrylate, isobutyl acrylate, dodecyl acrylate, n-octyl acrylate, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacrylate, dodecyl methacrylate, n-octyl methacrylate, phenyl methacrylate, α-chloromethyl methacrylate, benzyl methacrylate, methacrylonitrile, acrylonitrile, N-vinylpyrrolidone, N-vinylcarbazole, acrylic acid, methacrylic acid, acrylamide, methacrylic acid, amide, vinylpyridine, vinylpyrrolidone, vinylnaphthalene, vinyl fluoride, ethylene, 2-ethylhexyl acrylate, 2-ethylhexyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl acrylate, 2-hydroxypropyl methacrylate, 3-hydroxypropyl acrylate, 3-hydroxypropyl methacrylate, 3-hydroxybutyl acrylate, 3-hydroxybutyl methacrylate, 4-hydroxybutyl acrylate, 4-hydroxybutyl methacrylate, glycidyl acrylate, glycidyl methacrylate and mixtures thereof.

[0087] In yet another preferred embodiment of the present invention, the method for producing a polymer comprises at least vii) j) at least one transition metal catalyst; k) at least one reducing agent, and l) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: viii) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii); The degree of temperature change from the target temperature during step (ii) is in the range of −5.0% or more and +5.0% or less; The at least one free radically copolymerizable monomer is an ethylenically unsaturated monomer selected from the group consisting of styrene, butyl acrylate, methyl methacrylate, butyl methacrylate, 2-ethylhexyl acrylate, 2-ethylhexyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl acrylate, 2-hydroxypropyl methacrylate, 3-hydroxypropyl acrylate, 3-hydroxypropyl methacrylate, glycidyl methacrylate, and mixtures thereof.

[0088] In another preferred embodiment of the present invention, the method for producing a polymer comprises at least i) a) at least one transition metal catalyst; b) at least one reducing agent, and c) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: ii) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii); The at least one free-radically copolymerizable monomer is added intermittently or continuously.

[0089] In another preferred embodiment of the present invention, the method for producing a polymer comprises at least i) a) at least one transition metal catalyst; b) at least one reducing agent, and c) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: ii) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii); The degree of temperature change from the target temperature during step (ii) is in the range of -5.0% to +5.0%.

[0090] In another preferred embodiment of the present invention, the method for producing a polymer comprises at least i) a) at least one transition metal catalyst; b) at least one reducing agent, and c) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: ii) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii); The degree of temperature change from the target temperature during step (ii) is in the range of −5.0% or more and +5.0% or less; Step (ii) is carried out within a period ranging from 1 hour to 25 hours.

[0091] In another preferred embodiment of the present invention, the method for producing a polymer comprises at least i) a) at least one transition metal catalyst; b) at least one reducing agent, and c) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: ii) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii); The at least one transition metal catalyst is added in an amount ranging from 0.1 ppm to 250 ppm.

[0092] In yet another preferred embodiment of the present invention, the method for producing a polymer comprises at least i) a) at least one transition metal catalyst; b) at least one reducing agent, and c) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: ii) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, The at least one free radically polymerizable monomer is added at a rate ranging from 0.17 wt % / min to 0.83 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer in step (ii).

[0093] In yet another preferred embodiment of the present invention, the method for producing a polymer comprises at least iii) d) at least one transition metal catalyst; e) at least one reducing agent, and f) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: iv) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.17 wt % / min to 0.83 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii); The at least one free radically copolymerizable monomer is an ethylenically unsaturated monomer, and is selected from the group consisting of styrene, α-methylstyrene, methyl acrylate, ethyl acrylate, butyl acrylate, isobutyl acrylate, dodecyl acrylate, n-octyl acrylate, 2-chloroethyl acrylate, carboxyethyl acrylate, phenyl acrylate, benzyl acrylate, α-chloromethyl acrylate, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacrylate, dodecyl methacrylate, n-octyl methacrylate, 2-chloroethyl methacrylate, carboxyethyl methacrylate, phenyl methacrylate, α-chloromethyl methacrylate, benzyl methacrylate, methacrylonitrile, acrylonitrile, N-vinylpyrrolidone, N-vinylcarbazole, acrylic acid, methacrylic acid, acrylamide, methacrylamide, vinylpyridine, vinylpyrrolide. and mixtures thereof.

[0094] In yet another preferred embodiment of the present invention, the method for producing a polymer comprises at least v) g) at least one transition metal catalyst h) at least one reducing agent, and i) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: vi) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.17 wt % / min to 0.83 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii); The at least one free radically copolymerizable monomer is an ethylenically unsaturated monomer selected from the group consisting of styrene, butyl acrylate, methyl methacrylate, butyl methacrylate, 2-ethylhexyl acrylate, 2-ethylhexyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl acrylate, 2-hydroxypropyl methacrylate, 3-hydroxypropyl acrylate, 3-hydroxypropyl methacrylate, glycidyl methacrylate, and mixtures thereof.

[0095] In yet another preferred embodiment of the present invention, the method for producing a linear diblock polymer comprises at least i) a) at least one transition metal catalyst; b) at least one reducing agent, and c) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: ii) adding at least one free-radically copolymerizable monomer selected from hydroxyethyl acrylate or methyl acrylate to the polymerization mixture to obtain an acrylic polymer; Including, The at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer in step (ii).

[0096] In another preferred embodiment of the present invention, the method for producing a polymer comprises at least i) a) at least one transition metal catalyst; b) at least one reducing agent, and c) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: ii) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii); The temperature in step (ii) is maintained in the range of 35°C to 150°C.

[0097] In an embodiment of the invention, the polymer is obtained by the method described above. In a preferred embodiment of the invention, the polymer is a block copolymer, a linear polymer or copolymer, a branched polymer or copolymer, a brush polymer or copolymer, a star polymer or copolymer.

[0098] In another preferred embodiment of the invention, the polydispersity of the polymers obtained by the methods described herein ranges from 1.0 to 10. In a more preferred embodiment of the invention, the polydispersity of the polymers obtained by the methods described herein ranges from 1.0 to 5.0. In a most preferred embodiment of the invention, the polydispersity of the polymers obtained by the methods described herein ranges from 1.0 to 3.0. In a particularly most preferred embodiment of the invention, the polydispersity of the polymers obtained by the methods described herein ranges from 1.0 to 2.0, more preferably from 1.10 to 1.60. In both cases, the polydispersity is determined by gel permeation chromatography against polystyrene standards.

[0099] In a preferred embodiment of the present invention, the polymers obtained by the process described herein have a number average molecular weight (M) in the range of 100 g / mol to 1,000,000 g / mol, as determined by gel permeation chromatography against polystyrene standards. n In another preferred embodiment of the present invention, the polymer obtained by the process described herein has a number average molecular weight (M) in the range of 200 g / mol to 100,000 g / mol, as determined by gel permeation chromatography against polystyrene standards. n In a more preferred embodiment of the present invention, the polymer obtained by the process described herein has a number average molecular weight (M) in the range of 200 g / mol to 50,000 g / mol, inclusive, as determined by gel permeation chromatography against polystyrene standards. n In the most preferred embodiment of the present invention, the polymer obtained by the process described herein has a number average molecular weight (M) in the range of 500 g / mol to 50,000 g / mol, inclusive, as determined by gel permeation chromatography against polystyrene standards. n ).

[0100] Embodiment Below, a list of embodiments is provided to further illustrate the present disclosure, but is not intended to limit the disclosure to the specific embodiments listed below.

[0101] 1. A method for producing a polymer, comprising: i) a) at least one transition metal catalyst; b) at least one reducing agent, and c) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: ii) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, The process wherein the at least one free radically polymerizable monomer is added at a rate ranging from 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer of step (ii).

[0102] 2.a) The process according to embodiment 1, wherein the at least one transition metal catalyst is a transition metal halide catalyst.

[0103] 3. The process according to embodiment 2, wherein the transition metal halide catalyst is selected from the group consisting of iron chloride, iron bromide, iron iodide, iron(0), ruthenium chloride, ruthenium bromide, ruthenium iodide, copper chloride, copper bromide, copper iodide, and copper(0).

[0104] 4.b) The method according to embodiment 1, wherein the at least one reducing agent is selected from the group consisting of stannous 2-ethylhexanoate, sulfites, bisulfites, thiosulfites, mercaptans, hydroxylamines, amines, hydrazine, phenylhydrazine, hydrazones, hydroquinones, food preservatives, flavonoids, beta-carotene, vitamin A, C-tocopherol, vitamin E, propyl gallate, octyl gallate, propionic acid, ascorbic acid, sorbates, reducing sugars, sugars containing aldehyde groups, glucose, lactose, fructose, dextrose, potassium tartrate, nitrites, dextrins, aldehydes, glycine and antioxidants.

[0105] 5.b) The method according to embodiment 1, wherein the at least one reducing agent is a free radical initiator.

[0106] 6. The free radical initiator is ammonium persulfate, hydrogen peroxide, acetyl peroxide, cumyl peroxide, tert-butyl peroxide, propionyl peroxide, benzoyl peroxide, chlorobenzoyl peroxide, dichlorobenzoyl peroxide, bromomethylbenzoyl peroxide, lauroyl peroxide, sodium persulfate, potassium persulfate, diisopropyl peroxycarbonate, tetralin hydroperoxide, 1-phenyl-2-methylpropyl-1-hydroperoxide, tert-butyl pertriphenylacetate hydroperoxide, tert-butyl performate, tert-butyl peracet ... t-Butyl, tert-butyl perbenzoate, tert-butyl perphenylacetate, tert-butyl permethoxyacetate, tert-butyl per-N-(3-tolyl)carbamate, 2,2'-azobispropane, 2,2'-dichloro-2,2'-azobispropane, 1,1'-azo(methylethyl)diacetate, 2,2'-azobis(2-amidinopropane)hydrochloride, 2,2'-azobis(2-amidinopropane)nitrate, 2,2'-azobisisobutane, 2,2'-azobisisobutyramide, 2,2'-azobisisobutyronitrile, 2,2'-azobi 2,2'-Azobis-2-methylpropionate, 2,2'-dichloro-2,2'-azobisbutane, 2,2'-azobis-2-methylbutyronitrile, 2,2'-azobis-2-methylpropionitrile, 2-bromoisobutyric acid ethyl, 2,2'-azobisisobutyric acid dimethyl, 1,1'-azobis(1-methylbutyronitrile-3-sodium sulfonate, 2-(4-methylphenylazo)-2-methylmalonodinitrile, 4,4'-azobis-4-cyanovaleric acid, 3,5-dihydroxymethylphenylazo-2-methylmalonodinitrile, 2-(4-bromo Phenylazo)-2-allylmalonodinitrile, 2,2'-azobis-2-methylvaleronitrile, 4,4'-azobis-4-dimethylcyanovalerate, 2,2'-azobis-2,4-dimethylvaleronitrile, 2,2'-azobis-4-methoxy-2,4-dimethylvaleronitrile, 1,1'-azobiscyclohexanenitrile, 2,2'-azobis-2-propylbutyronitrile, 1,1'-azobis-chlorophenylethane, 1,1'-azobis-1-cyclohexanecarbonitrile, 1,1'-azobis-1-cycloheptanenitrile, 1,The process according to embodiment 5, wherein the aryl group is selected from the group consisting of 1'-azobis-1-phenylethane, 1,1'-azobiscumene, ethyl 4-nitrophenylazobenzylcyanoacetate, phenylazodiphenylmethane, phenylazotriphenylmethane, 4-nitrophenylazotriphenylmethane, 1'-azobis-1,2-diphenylethane, poly(bisphenol 4,4'-azobis-4-cyanopentanoate), poly(tetraethylene glycol 2,2'-azobisisobutyrate), 1,4-bis(pentaethylene)-2-tetrazene, 1,4-dimethoxycarbonyl-1,4-diphenyl-1-2-tetrazene and mixtures thereof.

[0107] 7.c) The process according to embodiment 1, wherein the at least one atom transfer radical polymerization initiator is selected from the group consisting of sulfonyl halides, alkyl halides and substituted alkyl halides.

[0108] 8. The method according to embodiment 7, wherein the alkyl halides and substituted alkyl halides are selected from the group consisting of benzyl bromide, benzyl chloride, ethyl bromoacetate, diethyl 2-bromo-2-methylmalonate, ethyl 2-bromoisobutyrate, methyl 2-bromopropionate, ethyl 2-chloroisobutyrate, and 1,2-bis(2-bromoisobutyryloxy)ethane.

[0109] 9. The method according to embodiment 1, wherein at least one free-radically copolymerizable monomer is an ethylenically unsaturated monomer.

[0110] 10. The ethylenically unsaturated monomer is styrene, α-methylstyrene, methyl acrylate, ethyl acrylate, butyl acrylate, isobutyl acrylate, dodecyl acrylate, n-octyl acrylate, 2-chloroethyl acrylate, carboxyethyl acrylate, phenyl acrylate, benzyl acrylate, α-chloromethyl acrylate, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacrylate, dodecyl methacrylate, n-octyl methacrylate, 2-chloroethyl methacrylate, methacrylate Carboxyethyl acrylate, Phenyl methacrylate, α-chloromethyl methacrylate, Benzyl methacrylate, Butadiene, Isoprene, Methacrylonitrile, Acrylonitrile, Vinyl methyl ether, Vinyl isobutyl ether, Vinyl ethyl ether, Vinyl acetate, Vinyl propionate, Vinyl benzoate, Vinyl butyrate, Vinyl methyl ketone, Vinyl hexyl ketone, Methyl isopropenyl ketone, Vinylidene chloride, Vinylidene chlorofluoride, N-Vinylpyrrolidone, N-Vinylcarbazole, Acrylic acid, Methacrylic acid, Acrylic acid amide, methacrylamide, vinylpyridine, vinylpyrrolidone, vinyl-N-methylpyridinium chloride, vinylnaphthalene, p-chlorostyrene, vinyl chloride, vinyl bromide, vinyl fluoride, ethylene, propylene, butylene, isobutylene, 2-ethylbutyl acrylate, 2-ethylbutyl methacrylate, 2-ethylhexyl acrylate, 2-ethylhexyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl acrylate, 2-hydroxypropyl methacrylate, 10. The process according to embodiment 9, wherein the hydroxypropyl acrylate is selected from the group consisting of 3-hydroxypropyl acrylate, 3-hydroxypropyl methacrylate, 3-hydroxybutyl acrylate, 3-hydroxybutyl methacrylate, 4-hydroxybutyl acrylate, 4-hydroxybutyl methacrylate, 6-hydroxyhexyl acrylate, 6-hydroxyhexyl methacrylate, 3-hydroxy-2-ethylhexyl acrylate, 3-hydroxy-2-ethylhexyl methacrylate, glycidyl acrylate, glycidyl methacrylate, and mixtures thereof.

[0111] 11. The ethylenically unsaturated monomer is styrene, α-methylstyrene, methyl acrylate, ethyl acrylate, butyl acrylate, isobutyl acrylate, dodecyl acrylate, n-octyl acrylate, 2-chloroethyl acrylate, carboxyethyl acrylate, phenyl acrylate, benzyl acrylate, α-chloromethyl acrylate, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacrylate, dodecyl methacrylate, n-octyl methacrylate, 2-chloroethyl methacrylate, carboxyethyl methacrylate, phenyl methacrylate, α-chloromethyl methacrylate, benzyl methacrylate, methacrylonitrile, acrylonitrile, N-vinylpyrrolidone, N-vinylcarbazole, acrylic acid, methacrylic acid, acrylamide, methacrylamide, vinylpyridine, vinylpyrrolidone, vinyl chloride-N-methylpyridinyl chloride 11. The process according to embodiment 10, wherein the vinyl monomer is selected from the group consisting of vinyl acrylate, vinyl naphthalene, vinyl fluoride, ethylene, 2-ethylbutyl acrylate, 2-ethylbutyl methacrylate, 2-ethylhexyl acrylate, 2-ethylhexyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl acrylate, 2-hydroxypropyl methacrylate, 3-hydroxypropyl acrylate, 3-hydroxypropyl methacrylate, 3-hydroxybutyl acrylate, 3-hydroxybutyl methacrylate, 4-hydroxybutyl acrylate, 4-hydroxybutyl methacrylate, 6-hydroxyhexyl acrylate, 6-hydroxyhexyl methacrylate, 3-hydroxy-2-ethylhexyl acrylate, 3-hydroxy-2-ethylhexyl methacrylate, glycidyl acrylate, glycidyl methacrylate and mixtures thereof.

[0112] 12. The ethylenically unsaturated monomer is styrene, α-methylstyrene, methyl acrylate, ethyl acrylate, butyl acrylate, isobutyl acrylate, dodecyl acrylate, n-octyl acrylate, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacrylate, dodecyl methacrylate, n-octyl methacrylate, phenyl methacrylate, α-chloromethyl methacrylate, benzyl methacrylate, methacrylonitrile, acrylonitrile, N-vinylpyrrolidone, N-vinylcarbazole, acrylic acid, methacrylic acid, acrylamide, methacrylamide, vinylpyridine, vinylpyrrolidone ... The process according to embodiment 10, wherein the vinyl acrylate or vinyl naphthalene is selected from the group consisting of vinyl fluoride, ethylene, 2-ethylhexyl acrylate, 2-ethylhexyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl acrylate, 2-hydroxypropyl methacrylate, 3-hydroxypropyl acrylate, 3-hydroxypropyl methacrylate, 3-hydroxybutyl acrylate, 3-hydroxybutyl methacrylate, 4-hydroxybutyl acrylate, 4-hydroxybutyl methacrylate, glycidyl acrylate, glycidyl methacrylate and mixtures thereof.

[0113] 13. The process according to embodiment 10, wherein the ethylenically unsaturated monomer is selected from the group consisting of styrene, butyl acrylate, methyl methacrylate, butyl methacrylate, 2-ethylhexyl acrylate, 2-ethylhexyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl acrylate, 2-hydroxypropyl methacrylate, 3-hydroxypropyl acrylate, 3-hydroxypropyl methacrylate, glycidyl methacrylate, and mixtures thereof.

[0114] 14. The process according to any of the preceding embodiments, wherein the at least one free-radically copolymerizable monomer is added intermittently or continuously.

[0115] 15. The process according to any of the preceding embodiments, wherein the molar ratio of the at least one free-radically copolymerizable monomer to the at least one transition metal catalyst is in the range of ≧10:1.0 to ≦500,000:1.0.

[0116] 16. The method according to any of the preceding embodiments, wherein the molar ratio of the at least one free radically copolymerizable monomer to the at least one atom transfer radical polymerization initiator is in the range of ≧1.0:1.0 to ≦10,000:1.0.

[0117] 17. The method according to any of the preceding embodiments, wherein the molar ratio of the at least one transition metal catalyst to the at least one atom transfer radical polymerization initiator is in the range of ≧0.0005:1.0 to ≦50:1.0.

[0118] 18. The method according to any of the preceding embodiments, wherein the molar ratio of the at least one free radical initiator to the at least one atom transfer radical polymerization initiator is in the range of ≧0.005:1.0 to ≦50:1.0.

[0119] 19. The method according to any of the preceding embodiments, wherein the polymerization mixture further comprises at least one solvent.

[0120] 20. The method according to embodiment 19, wherein the at least one solvent is selected from the group consisting of methanol, ethanol, n-propanol, isopropanol, butanol, butoxyethanol, acetone, butanone, pentanone, hexanone, methyl ethyl ketone, methyl isobutyl ketone, ethyl acetate, butyl acetate, amyl acetate, methoxypropyl acetate, tetrahydrofuran, diethyl ether, ethylene glycol, polyethylene glycol, and mixtures thereof.

[0121] 21. The process according to any of the preceding embodiments, wherein step ii) is carried out as a two-phase, emulsion, mini-emulsion, micro-emulsion, inverse emulsion or suspension polymerization process.

[0122] 22. The method according to any of the preceding embodiments, wherein the at least one free radically polymerizable monomer is added at a rate ranging from 0.17 wt % / min to 0.83 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer.

[0123] 23. The method according to any of the preceding embodiments, wherein the at least one free radically polymerizable monomer is added at a rate ranging from 0.25 wt% / min to 0.5 wt% / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer.

[0124] 24. The method according to any of the preceding embodiments, wherein the polymerization of at least one free-radically polymerizable monomer into a polymer allows for at least 90% conversion of the total free-radically polymerizable monomer.

[0125] 25. The method according to any of the preceding embodiments, wherein the temperature in step ii) is maintained in the range of ≧35° C. to ≦150° C.

[0126] 26. The method according to any one of embodiments 1 to 25, wherein the degree of temperature change from the target temperature in step (ii) is in the range of ≧−10.0% to ≦+10.0%.

[0127] 27. The method according to any of the preceding embodiments, wherein step (ii) is carried out within a period ranging from 1 hour to 25 hours.

[0128] While the invention has been described in terms of specific embodiments thereof, certain modifications and equivalents will be apparent to those skilled in the art and are intended to be included within the scope of the invention. EXAMPLES

[0129] The present invention is illustrated in detail by the following non-limiting examples. More specifically, the test methods specified below are part of the general disclosure of this application and are not limited to the specific examples.

[0130] Polymer / copolymer manufacturing According to methods well known to those skilled in the art, diblock copolymers (copolymer I, copolymer II and polymer IV) were synthesized by the ultra-high controlled radical polymerization (CRP) or ultra-high ATRP process described below. The composition of the raw materials is shown in Tables 1, 3 and 7. The properties of the copolymers of the present invention synthesized are shown in Tables 2, 4 and 8.

[0131] [Example 1] Preparation of diblock copolymer I Diblock copolymer I was synthesized in two steps by ultra-high ATRP. In the first step, glycidyl methacrylate (GMA) was polymerized to obtain polyglycidyl methacrylate (polyGMA) with active chain ends as the first block. This was followed by ultra-high ATRP of a mixture of butyl acrylate (BMA), butyl acrylate (BA) and 2-hydroxypropyl methacrylate (HPMA) as described below. The composition of the raw materials is shown in Table 1. The temperature profile was monitored by the KEM-NET controller, as illustrated in Figure 1. The monomer conversion was measured by NMR and gas chromatography, as illustrated in Figure 2.

[0132] Step A: Reagents 1-2 (Table 1) were introduced into a 3 L 4-neck round bottom flask equipped with a nitrogen line, condenser, stirrer, heating mantle and thermocouple. Reagents 3-5 (Table 1) were mixed and stirred in a 20 mL sintered vial to produce a bluish green homogenous catalyst solution, and the solution was added to the reaction flask. The solution was heated to 80°C under a nitrogen blanket. When the temperature reached 80°C, mixtures 6-7 (Table 1) were added to the flask in one portion. When the temperature rose again to 80°C, monomer (GMA) 8 (Table 1) was fed to the reaction flask using a monomer pump. The feeds were run at 80°C for a total of 2.5 hours, then the temperature was held at 80°C for an additional hour.

[0133] Step B: At the end of step A, the solvent (n-butyl acetate) 9 (Table 1) was added in one portion. The temperature was allowed to drop slightly. When the temperature reached 80°C again, a mixture of 10 and 11 (Table 1) was added in one portion to the flask. The temperature was allowed to drop slightly and reach 80°C. At this point, a monomer mixture of 12-14 (Table 1) was fed at a constant rate through the monomer pump. The feed was terminated in 3 hours, and then the reaction was held at 80°C for 1 hour. The temperature was then gradually increased to 90°C and held for an additional hour. Monomer conversion reached >99% and was analyzed by NMR.

[0134] [Table 1]

[0135] where n-Butyl acetate was obtained from Nexeo Solutions LLC. TsCl = p-toluenesulfonyl chloride was obtained from Sigma Aldrich. TPMA = tris(2-pyridylmethyl)amine was obtained from Sigma Aldrich. CuCl 2 = Copper chloride and MeOH = Methanol were obtained from Sigma Aldrich. AMBN = 2,2'-azobis(2-methylbutyronitrile) was obtained from Akzo Nobel Coatings INC. Glycidyl methacrylate was obtained from Dow Chemical. n-Butyl acrylate and butyl methacrylate were obtained from BASF Corporation. HPMA = 2-hydroxypropyl methacrylate was obtained from Dow Chemical.

[0136] Monomer addition rates for the synthesis of copolymer I: step A=0.67 wt % / min and step B=0.55 wt % / min.

[0137] As also shown in FIG. 1, the degree of temperature change from the target temperature during the monomer addition period during this process ranges from −2.1° C. to +2.3° C., or in other words, from −2.6% to +2.9%.

[0138] [Table 2]

[0139] [Example 2] Preparation of diblock copolymer II Diblock copolymer II was synthesized in two steps by ultra-high ATRP. In the first step, glycidyl methacrylate (GMA) was polymerized to obtain polyglycidyl methacrylate (polyGMA) with active chain ends as the first block. This was followed by ultra-high ATRP of a mixture of butyl methacrylate (BMA), butyl acrylate (BA) and 2-hydroxypropyl methacrylate (HPMA) as described below. The composition of the raw materials is shown in Table 3. The temperature profile was monitored by the KEM-NET controller, as illustrated in Figure 3. The monomer conversion was measured by NMR and gas chromatography, as illustrated in Figure 4.

[0140] Step A: Reagents 1-2 (Table 3) were introduced into a 3 L 4-neck round bottom flask equipped with a nitrogen line, condenser, stirrer, heating mantle and thermocouple. Reagents 3-5 (Table 3) were mixed and stirred in a 20 mL sintered vial to produce a bluish green homogenous catalyst solution, and the solution was added to the reaction flask. The solution was heated to 73°C under a nitrogen blanket. When the temperature reached 73°C, mixtures 6-7 (Table 3) were added to the flask in one portion. When the temperature again rose to 73°C, monomer (GMA) 8 (Table 3) was fed to the reaction flask using a monomer pump. The feeds were run at 73°C for a total of 3.33 hours, then the temperature was held at 73°C for an additional hour.

[0141] Step B: At the end of step A, the solvent (n-butyl acetate) 9 (Table 3) was added in one portion. The temperature was allowed to drop slightly. When the temperature again reached 73°C, a mixture of 10 and 11 (Table 3) was added in one portion to the flask. The temperature was allowed to drop slightly and reach 73°C. At this point, a monomer mixture of 12-14 (Table 3) was fed at a constant rate through the monomer pump. The feeds were terminated at 3.5 hours, and then the reaction was held at 73°C for 0.5 hours. The temperature was then gradually increased to 90°C and held for an additional hour. Monomer conversion reached >99% and was analyzed by NMR.

[0142] [Table 3]

[0143] where n-Butyl acetate was obtained from Nexeo Solutions LLC. TsCl = p-toluenesulfonyl chloride was obtained from Sigma Aldrich. TPMA = tris(2-pyridylmethyl)amine was obtained from Sigma Aldrich. CuCl 2 = Copper chloride and MeOH = Methanol were obtained from Sigma Aldrich. AMBN = 2,2'-azobis(2-methylbutyronitrile) was obtained from Akzo Nobel Coatings INC. Glycidyl methacrylate was obtained from Dow Chemical. n-Butyl acrylate and butyl methacrylate were obtained from BASF Corporation. HPMA = 2-hydroxypropyl methacrylate was obtained from Dow Chemical.

[0144] Monomer addition rates for the synthesis of copolymer II: Step A=0.50 wt % / min and Step B=0.48 wt % / min.

[0145] As also shown in FIG. 3, the degree of temperature change from the target temperature during the monomer addition period during this process ranges from −2.2° C. to +2.3° C., or in other words, from −3.0% to +3.2%.

[0146] [Table 4]

[0147] [Comparative Example 1] Preparation of diblock copolymer III Diblock copolymer III was synthesized in two steps by traditional ATRP. In the first step, glycidyl methacrylate (GMA) was polymerized to obtain polyglycidyl methacrylate (polyGMA) with active chain ends as the first block. This was followed by traditional ATRP of a mixture of butyl methacrylate (BMA), butyl acrylate (BA) and 2-hydroxypropyl methacrylate (HPMA) as described below. The composition of the raw materials is shown in Table 5. The temperature profile was monitored by the KEM-NET controller, as illustrated in Figure 5. Monomer conversion was measured by NMR and gas chromatography, as illustrated in Figure 6.

[0148] Step A: Reagents 1-3 (Table 5) were introduced into a 3 L 4-neck round bottom flask equipped with a nitrogen line, condenser, stirrer, heating mantle and thermocouple. Reagents 3-5 (Table 5) were mixed and stirred in a 20 mL sintered vial to produce a bluish green homogenous catalyst solution and the solution was added to the reaction flask. The solution was heated to 73°C under a nitrogen blanket. When the temperature reached 73°C, mixture 6-7-8 (Table 5) was added to the flask in one portion. The mixture was held at 73°C for a total of 3.33 hours.

[0149] Step B: At the end of step A, mixtures 9-12 (Table 5) were added in one portion. When the temperature again reached 73°C, mixtures 13-14 (Table 5) were added in one portion to the flask. The temperature immediately dropped slightly and was allowed to reach 73°C by applying external heat from a heating mantle. Within minutes, a self-accelerating exotherm began and the temperature rose to 85°C in less than 10 minutes. With no heat supply and application of cooling air, the temperature dropped slightly. However, when the cooling air was stopped, the temperature rose again. The exotherm was not controlled without the application of cooling air. Therefore, the cooling air was continued and the temperature was maintained at 73°C-90°C. A total of 2 hours after the addition of reducing agents 13-14 (Table 5), the temperature dropped below 73°C. Monomer conversion reached approximately 95% and was analyzed by NMR. The reaction was continued at 80°C for an additional 1.5 hours.

[0150] [Table 5]

[0151] where n-Butyl acetate was obtained from Nexeo Solutions LLC. TsCl = p-toluenesulfonyl chloride was obtained from Sigma Aldrich. TPMA = tris(2-pyridylmethyl)amine was obtained from Sigma Aldrich. CuCl 2 = Copper chloride and MeOH = Methanol were obtained from Sigma Aldrich. AMBN = 2,2'-azobis(2-methylbutyronitrile) was obtained from Akzo Nobel Coatings INC. Glycidyl methacrylate was obtained from Dow Chemical. n-Butyl acrylate and butyl methacrylate were obtained from BASF Corporation. HPMA = 2-hydroxypropyl methacrylate was obtained from Dow Chemical.

[0152] Monomer addition rates for the synthesis of copolymer III: Step A=100 wt % / min and Step B=100 wt % / min.

[0153] The extent of temperature variation from the target temperature during the monomer conversion period during this process ranged from -2.3°C to +16°C, or in other words -3.2% to +22.0%, as shown in Figure 5. Cooling air was applied to prevent further increase in solution temperature from the set temperature during the exotherm.

[0154] [Table 6]

[0155] [Example 3] Preparation of Polymer IV Polymerization of 2-hydroxyethyl acrylate (HEA) was carried out using the ultra-advanced ATRP method. The composition of the feedstock is shown in Table 7. The temperature profile was monitored by the KEM-NET controller, as illustrated in Figure 7. The monomer conversion was measured by NMR and gas chromatography, as illustrated in Figure 8.

[0156] Procedure: Reagents 1-2 (Table 7) were introduced into a 1 L 4-neck round bottom flask equipped with a nitrogen line, condenser, stirrer, heating mantle and thermocouple. Reagents 3-5 (Table 7) were mixed and stirred in a 20 mL sintered vial to produce a bluish green homogenous catalyst solution, and the solution was added to the reaction flask. The solution was heated to 60°C under a nitrogen blanket. When the temperature reached 60°C, mixtures 6-7 (Table 7) were added to the flask in one portion. When the temperature again reached 60°C, monomer 8 (HEA) (Table 7) was fed to the reaction flask using a monomer pump. The feed was carried out at 60°C for a total of 3 hours, then the temperature was held at 60°C for an additional hour.

[0157] [Table 7]

[0158] where Propylene glycol n-propyl ether was obtained from Nexeo Solutions LLC. EBiB = Ethyl 2-bromoisobutyrate was obtained from Sigma Aldrich. TPMA = tris(2-pyridylmethyl)amine was obtained from Sigma Aldrich. CuCl 2 = Copper chloride and MeOH = Methanol were obtained from Sigma Aldrich. VAZO-52= was obtained from Chemours Company. MEK = methyl ethyl ketone was obtained from Nexeo Solutions LLC. HEA = 2-hydroxyethyl acrylate was obtained from Rohm and Haas Chemicals LLC.

[0159] Monomer addition rate for synthesis of polymer IV: 0.55 wt% / min.

[0160] As shown in FIG. 7, the degree of temperature change from the target temperature during the monomer addition period ranges from −1° C. to +3.5° C., or in other words, from −1.67% to +5.8%.

[0161] [Table 8]

[0162] [Comparative Example 2] Preparation of Polymer V The polymerization of 2-hydroxyethyl acrylate (HEA) was carried out using the traditional ATRP method. The composition of the raw materials is shown in Table 9. The temperature profile was monitored by the KEM-NET controller, as illustrated in Figure 9.

[0163] Procedure: Reagents 1-3 (Table 9) were introduced into a 1 L 4-neck round bottom flask equipped with a nitrogen line, condenser, stirrer, heating mantle and thermocouple. Reagents 4-6 (Table 9) were mixed and stirred in a 20 mL sintered vial to produce a bluish green homogeneous catalyst solution, and the solution was added to the reaction flask. The solution was heated to 60°C under a nitrogen blanket. When the temperature reached 60°C, mixtures 7-8 (Table 9) were added to the flask in one portion. An excessively exothermic reaction was immediately evident, so the polymerization was quenched with a benzothiazine inhibitor and cooled air.

[0164] [Table 9]

[0165] where Propylene glycol n-propyl ether was obtained from Nexeo Solutions LLC. EBiB = Ethyl 2-bromoisobutyrate was obtained from Sigma Aldrich. TPMA = tris(2-pyridylmethyl)amine was obtained from Sigma Aldrich. CuCl 2 = Copper chloride and MeOH = Methanol were obtained from Sigma Aldrich. VAZO-52= was obtained from Chemours Company. MEK = methyl ethyl ketone was obtained from Nexeo Solutions LLC. HEA = 2-hydroxyethyl acrylate was obtained from Rohm and Haas Chemicals LLC.

[0166] Monomer addition rate for the synthesis of polymer V: 100 wt% / min.

[0167] As shown in FIG. 9, the degree of temperature change from the target temperature during the monomer conversion in this process ranges from −43.2° C. to +17.8° C., or from −72.1% to +30.0%.

[0168] [Example 4] Preparation of Diblock Copolymer VI (Example of the Invention) Diblock copolymer IV was synthesized in two steps by ultra-advanced ATRP. In the first step, styrene was polymerized to obtain polystyrene (pSt) with active chain ends as the first block. This was followed by ultra-advanced ATRP of a mixture of butyl acrylate (BA) and N-vinylcarbazole (NVCz) to produce pSt-block-p(BA-co-NVCz) as described below. The composition of the raw materials is shown in Table 10. The temperature profile was monitored by a Honeywell temperature controller, as illustrated in FIG. 10. Monomer conversion was measured by gas chromatography, as illustrated in Table 11.

[0169] Step A: Reagents 1-2 (Table 10) were introduced into a 1 L 4-neck round bottom flask equipped with a nitrogen line, condenser, stirrer, heating mantle and thermocouple. Reagents 3-5 (Table 10) were mixed and stirred in a 20 mL sintered vial to produce a bluish green homogenous catalyst solution and the solution was added to the reaction flask. The solution was heated to 110°C under a nitrogen blanket. When the temperature reached 110°C, mixtures 6-8 (Table 10) were added to the flask in one portion. When the temperature again reached 110°C, monomer (styrene) 8 (Table 10) was fed to the reaction flask using a monomer pump. The feeds were run at 110-120°C for a total of 3 hours, then the temperature was held at 125°C for an additional hour.

[0170] Step B: At the end of step A, the temperature was set to 120°C and a mixture of 10-11 (Table 10) was added in one go. The temperature was allowed to drop slightly. When the temperature reached 120°C again, a mixture of 12 and 13 (Table 10) was fed at a constant rate through the monomer pump for a total of 1 hour. The monomer conversion reached >79% and was analyzed by gas chromatography as illustrated in Table 11.

[0171] [Table 10]

[0172] where MIAK = methyl isoamyl ketone was obtained from Eastman. TsCl = p-toluenesulfonyl chloride was obtained from Sigma Aldrich. TPMA = tris(2-pyridylmethyl)amine was obtained from Sigma Aldrich. CuCl 2 = Copper chloride and MeOH = Methanol were obtained from Sigma Aldrich. ACHN = 1,1'-azobis(cyanocyclohexane) was obtained from Akzo Nobel Coatings INC. Dicumyl peroxide was obtained from Sigma Aldrich. Styrene was obtained from Sigma Aldrich. n-Butyl acrylate and butyl methacrylate were obtained from BASF Corporation. N-vinylcarbazole was obtained from Sigma Aldrich.

[0173] Monomer addition rates for the synthesis of copolymer I: step A=0.55 wt % / min and step B=1.66 wt % / min.

[0174] As also shown in FIG. 10, the degree of temperature change from the target temperature during the monomer addition period during this process ranges from −1° C. to +4° C., or in other words, from −0.83% to +3.3%.

[0175] [Table 11]

[0176] [Comparative Example 3] Preparation of Polymer VII The polymerization of styrene was carried out using traditional ATRP methodology. The composition of the raw materials is shown in Table 12. The temperature profile was monitored by a Honeywell temperature controller, as illustrated in FIG.

[0177] Procedure: Reagents 1-2 (Table 10) were introduced into a 1 L 4-neck round bottom flask equipped with a nitrogen line, condenser, stirrer, heating mantle and thermocouple. In a 20 mL sintered vial, reagents 3-5 (Table 10) were mixed and stirred to produce a bluish green homogeneous catalyst solution, and the solution was added to the reaction flask, followed by 9 (monomer). The solution was heated to 110°C under a nitrogen blanket. When the temperature reached 110°C, mixture 6-8 (Table 12) was added to the flask in one portion. An excessively exothermic reaction immediately appeared, so the polymerization was quenched with benzothiazine inhibitor and cooling air.

[0178] [Table 12]

[0179] where MIAK = methyl isoamyl ketone was obtained from Eastman. TsCl = p-toluenesulfonyl chloride was obtained from Sigma Aldrich. TPMA = tris(2-pyridylmethyl)amine was obtained from Sigma Aldrich. CuCl 2 = Copper chloride and MeOH = Methanol were obtained from Sigma Aldrich. ACHN = 1,1'-azobis(cyanocyclohexane) was obtained from Akzo Nobel Coatings INC. Dicumyl peroxide was obtained from Sigma Aldrich. Styrene was obtained from Sigma Aldrich.

[0180] As also shown in FIG. 12, the degree of temperature change from the target temperature during the monomer conversion period in this process is in the range of −2.0° C. to +17.0° C., or −1.8% to +15.5%.

[0181] Discussion of results The results of Tables 2, 4, 8 and 11 of Examples 1-4 of the present invention and Figures 1-4, 7-8 and 10-11 show that the method of the present invention allows for controlled polymerization of polymerizable monomers. The temperature profiles of the examples of the present invention shown in Figures 1, 3, 7 and 10 show very well controlled acrylic polymerization. The ultra-advanced ATRP method mimics the traditional semi-batch method of free radical polymerization, which is considered one of the safest methods for industrial-scale production. The monomer starvation state in the ultra-advanced ATRP method ensures that there is no explosion due to uncontrolled heat generation in the reactor. In contrast, in the experiments shown in Comparative Examples 1, 2 and 3, when traditional ATRP was performed or attempted to be performed, a self-accelerating exothermic state appeared. In the case of Comparative Example 1, it was possible to attenuate the exotherm by application of cooling air, while in the case of Comparative Example 2, where the highly reactive monomer HEA was used, an acrylic inhibitor was added to quickly stop the reaction. Thus, the method of the present invention is also suitable for highly reactive monomers such as 2-hydroxyethyl acrylate shown in Example 3, in contrast to the traditional ATRP used in Comparative Example 2. The method of the present invention provides better control of exothermic mitigation and eliminates the requirement of having a large amount of reactive olefin / styrene monomer in the reactor at a given time. Contrary to the concept of traditional ATRP, the results disclosed in this invention confirm that the method has negligible radical-radical termination and side reactions of polymer chain radicals and catalyst with inflowing oxygen. As shown in Tables 2, 4, 8 and 11, it is a surprising achievement that block copolymers with narrow polydispersity and good control of molecular weight can be obtained by this monomer starvation ATRP.

[0182] advantage (i) the methods described herein allow for the controlled polymerization of polymerizable monomers; (ii) the methods described herein provide excellent control of exotherm and prevent explosions due to uncontrolled exotherm during polymerization reactions; (iii) the methods described herein, unlike traditional controlled radical polymerization methods, allow for controlled exotherm even upon sequential addition of oxygen and inhibitor to the reaction mixture; (iv) the methods described herein can be carried out under air-sensitive conditions in existing plant settings; (v) the processes described herein provide good control of the molecular weight of the resulting polymer; (vi) the polymers obtained by the processes described herein have narrow polydispersities; (vii) the processes described herein can be carried out as semi-batch and continuous processes, making them suitable for industrial scale production; (viii) the processes described herein are suitable for the polymerization of highly reactive monomers without the risk of uncontrolled exotherm; (ix) the processes described herein can be carried out using low amounts of catalysts and initiators; (x) The process described herein is the safest method for carrying out large scale polymerization of highly reactive monomers.

[0183] Test Method Molecular weight determination The polymer molecular weight (M w , M n and M. p To determine the molecular weight distribution, number average molecular weight M, of the polymer sample, the fully dissolved molecules are fractionated on a porous column stationary phase. Tetrahydrofuran (THF) is used as the elution solvent. The stationary phase is a combination of Waters Styragel HR5, HR4, HR3 and HR2 columns. 5 mg of sample is added to 1.5 mL of elution solvent and filtered through a 0.5 μm filter. After filtration, 100 μl of the polymer sample solution is injected into the column at a flow rate of 1.0 ml / min. Separation occurs depending on the size of the polymer coil formed in the elution solvent. Small molecules diffuse more frequently into the pores of the column material and therefore stagnate more than larger molecules. Large molecules are therefore eluted faster than small molecules. The molecular weight distribution, number average molecular weight M, of the polymer sample is n , weight average molecular weight M w and maximum peak molecular weight M pwas calculated using chromatography software utilizing a calibration curve generated with the PL-Polymer Standard Kit, which contains a series of unbranched polystyrene standards of various molecular weights available from Polymer Laboratories.

[0184] Determination of polydispersity index (PDI) PDI is expressed by the formula M w / M n The PDI of the polymer samples was determined according to the following formula: where Mw is the weight average molecular weight and Mn is the number average molecular weight. The PDI of the polymer samples was calculated using chromatography software utilizing a calibration curve generated with the PL-Polymer Standard Kit, which contains a series of unbranched polystyrene standards of various molecular weights available from Polymer Laboratories.

[0185] Acetylation of Polymer IV (PolyHEA) of Example 3 At monomer conversion >99% in Example 3, polymer IV (polyHEA) was not soluble in THF as is. Therefore, for GPC analysis, polyHEA was acetylated by adding 10 equivalents of acetic anhydride and a catalytic amount of triethylamine to a mixture of 5 mg of polyHEA and 1.5 mL of THF. After stirring for 5 hours at room temperature, the solution was filtered through a 0.5 μm filter and analyzed by GPC to find that M w , M n and M. p It was decided.

[0186] Temperature profile measurement The reaction time versus temperature profiles for the synthesis of copolymers I-III and polymers IV-V were recorded using a temperature controller from a J-KEM Scientific Model 210 with KEM-NET software. A temperature probe was inserted inside the solution, which was connected to the controller. The controller was further connected to a computer equipped with KEM-NET software. The set temperature (desired reaction temperature) and observed temperature were recorded in the KEM-NET software and further plotted using Excel software.

[0187] Determination of monomer conversion Monomer conversion at various time intervals was monitored by removing aliquots at given times using a needle and syringe, which were then soaked in chloroform (CDCl) for copolymers I-III. 3 ) and DMSO-d for polymers IV and V. 6 This was dissolved in and analyzed in a Bruker Ultrashield 300MHz NMR spectrometer. 1 For copolymer VI, the monomer conversion was determined by analysis using a Supelco Equity 5 Capillary GC column L×ID 30 m×0.25 mm, d f Measurements were performed using an Agilent 6890N network gas chromatograph equipped with a 1.00 μm.

[0188] Residual monomer determination During the synthesis of copolymers I-III, the amount of "residual monomer / total monomer (%)" at a given time was determined by integrating the remaining olefinic signal of the monomer (5.2-6.5 ppm protons) against the aromatic signal (7.6-7.8 ppm protons) of p-toluenesulfonyl chloride (TsCl) as an internal standard, and then dividing this number by the theoretical number of protons of 100% added monomer for one equivalent of TsCl at each step. In the synthesis of polymer IV, the amount of "residual monomer / total monomer (%)" was determined by integrating the remaining olefinic signal of the monomer (5.2-6.5 ppm protons) against the aromatic signal (7.6-7.8 ppm protons) of p-toluenesulfonyl chloride (TsCl) as an internal standard, and then dividing this number by the theoretical number of protons of 100% added monomer for one equivalent of TsCl. 2 It was determined by integrating the remaining olefinic signals of 2-hydroxyethyl acrylate (protons at 5.2-6.5 ppm) against one set of signals (protons at 3.8-4.2 ppm) and then dividing this number by the theoretical number of protons for 100% added monomer for one equivalent of ethyl 2-bromoisobutyrate (EBiB). For copolymer VI, the conversion was measured by gas chromatography using MIBK as the internal standard and a calibration table made from three different ratios of MIBK to styrene; MIBK to butyl acrylate; and MIBK to N-vinylcarbazole.

Claims

1. A method for producing a polymer comprising at least i) a) at least one transition metal catalyst; b) at least one reducing agent, and c) at least one atom transfer radical polymerization initiator preparing a polymerization mixture comprising: ii) adding at least one free-radically copolymerizable monomer to the polymerization mixture to obtain a polymer; Including, The process wherein in step (ii), the at least one free radically polymerizable monomer is added at a rate in the range of 0.08 wt % / min to 1.66 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer.

2. The process of claim 1 , wherein a) the at least one transition metal catalyst is a transition metal halide catalyst.

3. 2. The method of claim 1, wherein the at least one reducing agent is selected from the group consisting of stannous 2-ethylhexanoate, sulfites, bisulfites, thiosulfites, mercaptans, hydroxylamines, amines, hydrazine, phenylhydrazine, hydrazones, hydroquinones, food preservatives, flavonoids, beta-carotene, vitamin A, C-tocopherol, vitamin E, propyl gallate, octyl gallate, propionic acid, ascorbic acid, sorbates, reducing sugars, sugars containing aldehyde groups, glucose, lactose, fructose, dextrose, potassium tartrate, nitrites, dextrins, aldehydes, glycine, and antioxidants.

4. 10. The method of claim 1, wherein b) the at least one reducing agent is a free radical initiator.

5. 2. The method of claim 1, wherein c) the at least one atom transfer radical polymerization initiator is selected from the group consisting of sulfonyl halides, alkyl halides and substituted alkyl halides.

6. The process according to any one of claims 1 to 5, wherein the at least one free-radically copolymerizable monomer is added intermittently or continuously.

7. The process of any one of claims 1 to 6, wherein the molar ratio of the at least one free-radically copolymerizable monomer to the at least one transition metal catalyst is in the range of 10:1.0 to 500,000:1.

0.

8. 7. The method of any one of claims 1 to 6, wherein the molar ratio of the at least one free radically copolymerizable monomer to the at least one atom transfer radical polymerization initiator is in the range of 1.0:1.0 to 10,000:1.

0.

9. The process according to any one of claims 1 to 6, wherein the molar ratio of the at least one transition metal catalyst to the at least one atom transfer radical polymerization initiator is in the range of 0.0005:1.0 to 50:1.

0.

10. 7. The method according to any one of claims 1 to 6, wherein the molar ratio of the at least one free radical initiator to the at least one atom transfer radical polymerization initiator is in the range of 0.005:1.0 to 50.0:1.

0.

11. The process of any one of claims 1 to 10, wherein the polymerization mixture further comprises at least one solvent.

12. 12. The method of any one of claims 1 to 11, wherein the at least one free radically polymerizable monomer is added at a rate in the range of 0.17 wt % / min to 0.83 wt % / min, inclusive, based on the total weight of the at least one free radically polymerizable monomer.

13. 13. The method according to any one of claims 1 to 12, wherein the temperature in step ii) is maintained in the range of ≧35°C and ≦150°C.

14. The method according to any one of claims 1 to 13, wherein the degree of temperature change from the target temperature in step (ii) is in the range of -10.0% or more and +10.0% or less.

15. At least one free radical copolymerizable monomer is selected from the group consisting of styrene, α-methylstyrene, methyl acrylate, ethyl acrylate, butyl acrylate, isobutyl acrylate, dodecyl acrylate, n-octyl acrylate, 2-chloroethyl acrylate, carboxyethyl acrylate, phenyl acrylate, benzyl acrylate, α-chloromethyl acrylate, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacrylate, dodecyl methacrylate, n-octyl methacrylate, 2-chloroethyl methacrylate, carboxyethyl acrylate, phenyl acrylate, benzyl acrylate, butyl, carboxyethyl methacrylate, phenyl methacrylate, α-chloromethyl methacrylate, benzyl methacrylate, butadiene, isoprene, methacrylonitrile, acrylonitrile, vinyl methyl ether, vinyl isobutyl ether, vinyl ethyl ether, vinyl acetate, vinyl propionate, vinyl benzoate, vinyl butyrate, vinyl methyl ketone, vinyl hexyl ketone, methyl isopropenyl ketone, vinylidene chloride, chlorovinylidene fluoride, N-vinylpyrrolidone, N-vinylcarbazole, acrylic acid, methacrylic acid , acrylamide, methacrylamide, vinylpyridine, vinylpyrrolidone, vinyl-N-methylpyridinium chloride, vinylnaphthalene, p-chlorostyrene, vinyl chloride, vinyl bromide, vinyl fluoride, ethylene, propylene, butylene, isobutylene, 2-ethylbutyl acrylate, 2-ethylbutyl methacrylate, 2-ethylhexyl acrylate, 2-ethylhexyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl acrylate, 2-hydroxypropyl methacrylate 2. The method of claim 1, wherein the monomer is selected from the group consisting of ethyl acrylate, 3-hydroxypropyl acrylate, 3-hydroxypropyl methacrylate, 3-hydroxybutyl acrylate, 3-hydroxybutyl methacrylate, 4-hydroxybutyl acrylate, 4-hydroxybutyl methacrylate, 6-hydroxyhexyl acrylate, 6-hydroxyhexyl methacrylate, 3-hydroxy-2-ethylhexyl acrylate, 3-hydroxy-2-ethylhexyl methacrylate, glycidyl acrylate, glycidyl methacrylate, and mixtures thereof.

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