IN-SITU FORMED POLYETHER POLYOLS,

PROCESSES FOR THEIR PREPARATION, AND PROCESSES FOR THE PREPARATION OF POLYURETHANE FOAMS

FIELD

[0001] The invention relates to in-situ formed polyether polyol blends, processes for preparing these in-situ formed polyether polyol blends, and processes for preparing viscoelastic polyurethane foams from these in-situ formed polyether polyol blends. The in- situ formed polyether polyol blends provide simpler formulation processes by eliminating the need for blending two or more polyols while being phase stable and maintaining good physical properties in polyurethane foams comprising these in-situ formed polyether polyol blends.

BACKGROUND

[0002] In-situ formed polyether polyol blends are important and/or highly desirable because they eliminate the need to blend two or more polyols. Phase stability of polyether polyol blends is important to maintain uniformity of the blends, consistency of their performance in making polyurethane foams and eliminate the need to keep the blends well mixed during transportation or before use. The in-situ formation of phase stable polyether polyol blends simplifies formulation processes and also makes polyether polyol blend formulations accessible when there is no capacity to separately store and/or blend together individual components.

[0003] The popularity of viscoelastic polyurethane foam, also referred to as memory foam or low resilience foam, has significantly increased in recent years as pillows, toppers or layers in mattresses and bed in a box foams. It is also used in other home and office furnishings as well as automotive applications..

SUMMARY

[0004] The n-situ formed polyether polyol blends have an overall functionality of 2 to 3 and an overall hydroxyl number of 40 to 220 mg KOH/g. These polyether polyol blends comprise: (a) a monol initiated oxyalkylene ether having a hydroxyl number of less than or equal to 56 mg KOH/g, and containing less than or equal to 20% by weight of copolymerized oxyethylene, based on the total weight of monol initiated oxyalkylene ether (a),

(b) a polyether polyol having a hydroxyl number of 20 to 240 mg KOH/g, a nominal functionality of 2 to 8, and containing at least 50% by weight of copolymerized oxyethylene, based on 100% by weight of component (b),

(c) a polyether polyol having a hydroxyl number of 80 to 220 mg KOH/g, a nominal functionality of 2, and containing from 5 to 45% by weight of copolymerized oxyethylene, based on the total weight of polyether polyol (c), and

(d) a polyether polyol having a hydroxyl number of 80 to 220 mg KOH/g, a nominal functionality of greater than 2 to 8, and containing 5 to 45% by weight of copolymerized oxyethylene, based on the total weight of polyether polyol (d), wherein the n-situ formed polyether polyol blend comprises 15 to 40% by weight of (a) the monol initiated oxyalkylene ether, 3 to 45% by weight of (b) the polyether polyol, 8 to 30% by weight of (c) the polyether polyol, and 20 to 60% by weight of (d) the polyether polyol, with the sum of the %’s by weight of components (a), (b), (c) and (d) totaling 100% by weight of the in-situ formed polyether polyol blend.

[0005] The processes of preparing the n-situ formed polyether polyol blend having an overall functionality of 2 to 3, and an overall hydroxyl number of 40 to 220 mg KOH/g, comprise:

I) introducing into a reaction vessel a mixture comprising:

(1 ) an initially charged starter (Si) comprising a monofunctional compound having a hydroxyl number of less than or equal to 80 mg KOH/g, and

(2) a double metal cyanide (DMC) catalyst;

II) feeding

(1 ) an epoxide comprising propylene oxide and ethylene oxide in a weight ratio of 100:0 to 80:20, into the reaction vessel;

III) allowing the epoxide and the initially charged starter (Si) to react and to polymerize by feeding the epoxide until the equivalent weight of the monofunctional compound is increased by at least 10% by weight and reaches a value between 1 ,500 and 6,000;

IV) feeding

(1 ) an epoxide comprising propylene oxide and ethylene oxide in a weight ratio of 50:50 to 20:80, while continuously adding

(2) a continuously added starter (Sc) having a nominal functionality of 2 to 8, and an equivalent weight of 28 to 400, into the reaction vessel;

V) completing addition of the continuously added starter (Sc);

VI) allowing the mixture to continue to polymerize in the reaction vessel thereby forming

(1 ) an intermediate in-situ formed polyether polyol blend which has an overall hydroxyl number of 10 to 200 mg KOH/g, an overall functionality of greater than 1 to 3, and which comprises

(a) a monol initiated oxyalkylene ether having a hydroxyl number of less than or equal to 56 mg KOH/g, and containing less than or equal to 20% by weight of copolymerized oxyethylene, based on 100% by weight of (a), and

(b) a polyether polyol having a hydroxyl number of 20 to 240 mg KOH/g, a nominal functionality of 2 to 8, and containing at least 50% by weight of copolymerized oxyethylene, based on the total weight of the polyether polyol (b),

VII) feeding

(1 ) an epoxide comprising propylene oxide and ethylene oxide in a weight ratio of from 95:5 to 55:45, while continuously adding

(2) a continuously added starter (Sc) having a nominal functionality of 2 to 8, and an equivalent weight of 28 to 100, into the reaction vessel;

VIII) completing addition of the continuously added starter (Sc) and epoxide thereby forming, in addition to the monol initiated oxyalkylene ether (a) and polyether polyol (b);

(c) a polyether polyol having a hydroxyl number of 80 to 220 mg KOH/g, a nominal functionality of 2, and containing 5 to 45% by weight of copolymerized oxyethylene, based on the total weight of the polyether polyol (c), and

(d) a polyether polyol having a hydroxyl number of 80 to 220 mg KOH/g, a nominal functionality of greater than 2 to 8, and containing 5 to 45% by weight of copolymerized oxyethylene, based on the total weight of the polyether polyol (d); wherein the in-situ formed polyether polyol blend comprises 15 to 40% by weight of (a) the monol initiated oxyalkylene ether, 3 to 45% by weight of (b) the polyether polyol, 8 to 30% by weight of (c) the polyether polyol, and 20 to 60% by weight of (d) the polyether polyol, with the sum of the %’s by weight of components (a), (b), (c) and (d) totaling 100% by weight of the in-situ formed polyether polyol blend.

[0006] The processes of preparing the viscoelastic flexible polyurethane foams comprise reacting:

(A) a diisocyanate and/or polyisocyanate component,

(B) an isocyanate-reactive component comprising:

(1 ) a in-situ formed polyether polyol blend having an overall hydroxyl number of 40 to 220 mg KOH/g, and an overall functionality of 2 to 3, which comprises: (a) a monol initiated oxyalkylene ether having a hydroxyl number of less than or equal to 56 mg KOH/g, and containing less than or equal to 20% by weight of copolymerized oxyethylene, based on the total weight of monol initiated oxyalkylene ether (a),

(b) a polyether polyol having a hydroxyl number of 20 to 240 mg KOH/g, a nominal functionality of 2 to 8, and containing at least 50% of copolymerized oxyethylene, based on 100% by weight of component (b),

(c) a polyether polyol having a hydroxyl number of 80 to 220 mg KOH/g, a nominal functionality of 2, and containing 5 to 45% by weight of copolymerized oxyethylene, based on the total weight of polyether polyol (c), and

(d) a polyether polyol having a hydroxyl number of 80 to 220 mg KOH/g, a nominal functionality of greater than 2 to 8, and containing 5 to 45% by weight of copolymerized oxyethylene, based on the total weight of polyether polyol (d); wherein the in-situ formed polyether polyol blend comprises 15 to 40% by weight of (a) the monol initiated oxyalkylene ether, 3 to 45% by weight of (b) the polyether polyol, 8 to 30% by weight of (c) the polyether polyol, and 20 to 60% by weight of (d) the polyether polyol, with the sum of the %’s by weight of components (a), (b), (c) and (d) totaling 100% by weight of the in- situ formed polyether polyol blend; in the presence of:

(C) a blowing agent;

(D) a catalyst; and

(E) a surfactant.

[0007] In one embodiment, the in-situ formed polyether polyol blends are phase stable blends. DETAILED DESCRIPTION

[0008] Various embodiments are described and illustrated in this specification to provide an overall understanding of the structure, function, properties, and use of the disclosed inventions. It is understood that the various embodiments described and illustrated in this specification are non-limiting and non-exhaustive. Thus, the invention is not limited by the description of the various non-limiting and non-exhaustive embodiments disclosed in this specification. The features and characteristics described in connection with various embodiments may be combined with the features and characteristics of other embodiments. Such modifications and variations are intended to be included within the scope of this specification. As such, the claims may be amended to recite any features or characteristics expressly or inherently described in, or otherwise expressly or inherently supported by, this specification. Further, Applicant(s) reserve the right to amend the claims to affirmatively disclaim features or characteristics that may be present in the prior art. Therefore, any such amendments comply with the requirements of 35 U.S.C. § 112 and 35 U.S.C. § 132(a). The various embodiments disclosed and described in this specification can comprise, consist of, or consist essentially of the features and characteristics as variously described herein.

[0009] Any patent, publication, or other disclosure material identified herein is incorporated by reference into this specification in its entirety unless otherwise indicated, but only to the extent that the incorporated material does not conflict with existing definitions, statements, or other disclosure material expressly set forth in this specification. As such, and to the extent necessary, the express disclosure as set forth in this specification supersedes any conflicting material incorporated by reference herein. Any material, or portion thereof, that is said to be incorporated by reference into this specification, but which conflicts with existing definitions, statements, or other disclosure material set forth herein, is only incorporated to the extent that no conflict arises between that incorporated material and the existing disclosure material. Applicant(s) reserves the right to amend this specification to expressly recite any subject matter, or portion thereof, incorporated by reference herein. [0010] In this specification, other than where otherwise indicated, all numerical parameters are to be understood as being prefaced and modified in all instances by the term "about", in which the numerical parameters possess the inherent variability characteristic of the underlying measurement techniques used to determine the numerical value of the parameter. At the very least, and not as an attempt to limit the application of the doctrine of equivalents to the scope of the claims, each numerical parameter described in the present description should at least be construed in light of the number of reported significant digits and by applying ordinary rounding techniques.

[0011] Also, any numerical range recited in this specification is intended to include all sub-ranges of the same numerical precision subsumed within the recited range. For example, a range of "1.0 to 10.0" is intended to include all sub-ranges between (and including) the recited minimum value of 1.0 and the recited maximum value of 10.0, that is, having a minimum value equal to or greater than 1.0 and a maximum value equal to or less than 10.0, such as, for example, 2.4 to 7.6. All end points of any range are included unless specified otherwise. Any maximum numerical limitation recited in this specification is intended to include all lower numerical limitations subsumed therein and any minimum numerical limitation recited in this specification is intended to include all higher numerical limitations subsumed therein. Accordingly, Applicant(s) reserves the right to amend this specification, including the claims, to expressly recite any sub-range subsumed within the ranges expressly recited herein. All such ranges are intended to be inherently described in this specification such that amending to expressly recite any such sub-ranges would comply with the requirements of 35 U.S.C. § 112 and 35 U.S.C. § 132(a).

[0012] The grammatical articles "one", "a", "an", and "the", as used in this specification, are intended to include "at least one" or "one or more", unless otherwise indicated. Thus, the articles are used in this specification to refer to one or more than one (i.e. , to "at least one") of the grammatical objects of the article. By way of example, "a component" means one or more components, and thus, possibly, more than one component is contemplated and may be employed or used in an implementation of the described embodiments. Further, the use of a singular noun includes the plural, and the use of a plural noun includes the singular, unless the context of the usage requires otherwise.

[0013] Equivalent weights and molecular weights given herein in Daltons (Da) are number average equivalent weights and number average molecular weights respectively, unless indicated otherwise, and were determined by GPC as described herein.

[0014] All number average and weight average, M _n and M , respectively, molecular weights herein were determined by gel-permeation chromatography (GPC) using a method based on DIN 55672-1 employing chloroform as the eluent with a mixed bed column (Agilent PL Gel; SDVB; 3 micron Pore diameter: 1xMixed-E + 5 micron Pore diameter: 2xMixed-D), refractive index (Rl) detection and calibrated with polyethylene glycol.

[0015] All hydroxyl numbers (i.e. OH numbers) herein were determined according to ASTM D4274-11 , and are reported in mg KOH/g monol or polyol, as the case may be. [0016] The molecular weight is the number average equivalent weight multiplied by the starter functionality. The hydroxyl number equals 56,100 divided by the equivalent weight.

[0017] As used herein, the term “nominal functionality” refers to the functionality of a polyether polyol which is based solely on the functionality of the starter compound or initiator used in preparing the polyether polyol. The nominal functionality is typically used to describe the functionality of a specific compound.

[0018] As used herein, the term “overall functionality” refers to the average number of reactive groups (e.g. hydroxyl, amine, etc.) which are present per molecule of the polyether polyol or polyether polyol blend being described. This term is typically used when either a polyether polyol is prepared from two or more starter compounds or initiators that have different functionalities and/or when a blend of polyether polyols is used in which the individual polyether polyols have different functionalities.

[0019] As used herein, the term “in-situ formed” with respect to a polyether polyol blend means producing the polyether polyol blend during the course of an alkoxylation reaction in which at least one epoxide is added to a mixture of an initial starter (Si) and alkoxylation catalyst to initiate the alkoxylation and then at least one continuous starter (Sc) feed is added during the course of the alkoxylation to form a blend of polyether polyols that can vary in molecular weight and functionality.

[0020] Isocyanate index is the relative stoichiometric amount of isocyanate functional groups necessary to react with the isocyanate reactive groups present in the overall foam formulation. It is expressed as a percentage in this application; thus equal stoichiometric amounts of isocyanate functional groups and isocyanate reactive functional groups in the formulation provide an isocyanate index of 100%.

[0021] As used herein, the term “phase stable” means that the in-situ formed polyether polyol blends are stable to visual sedimentation, separation, agglomeration or “layering” for minimally about 30 days of storage days at 20°C or greater with no mixing and may range in transparency from clear to milky. Many of the preferred in-situ formed polyether polyol blends of this invention are phase stable for significantly longer time periods.

[0022] The in-situ formed polyether polyol blend having an overall functionality of 2 to 3, an overall hydroxyl number of 40 to 220 mg KOH/g, comprises: (a) a monol initiated oxyalkylene ether having a hydroxyl number of less than or equal to 56 mg KOH/g, and containing less than or equal to 20% by weight of copolymerized oxyethylene, based on the total weight of monol initiated oxyalkylene ether (a); (b) a polyether polyol having a hydroxyl number of 20 to 240 mg KOH/g, a nominal functionality of 2 to 8, and containing at least 50% by weight of copolymerized oxyethylene, based on 100% by weight of component (b); (c) a polyether polyol having a hydroxyl number of 80 to 220 mg KOH/g, a nominal functionality of 2, and containing 5 to 45% by weight of copolymerized oxyethylene, based on the total weight of polyether polyol (c); (d) a polyether polyol having a hydroxyl number of 80 to 220 mg KOH/g, a nominal functionality of greater than 2 to 8, and containing 5 to 45% by weight of copolymerized oxyethylene, based on the total weight of polyether polyol (d); wherein the in-situ formed polyether polyol blend comprises 15 to 40% by weight of (a) the monol initiated oxyalkylene ether, 3 to 45% by weight of (b) the polyether polyol, 8 to 30% by weight of (c) the polyether polyol, and 20 to 60% by weight of (d) the polyether polyol, with the sum of the %’s by weight of components (a), (b), (c) and (d) totaling 100% by weight of the in-situ formed polyether polyol blend.

[0023] Suitable monol initiated oxyalkylene ethers (a) have a hydroxyl number of less than or equal to 56 mg KOH/g and contain less than or equal to 20% by weight of copolymerized oxyethylene. These monols have a hydroxyl number of less than or equal to 56 mg KOH/g, or of less than or equal to 28 mg KOH/g.

[0024] Suitable starters for (a) include polyoxyalkylene monols formed by addition of multiple equivalents of epoxide to a low equivalent weight monofunctional starter. Low equivalent weight monofunctional starters useful herein may be linear or branched compounds, and/or may be naturally-derived or synthetic compounds. Some suitable low equivalent weight monofunctional starters include compounds such as, for example, methanol, ethanol, phenols, allyl alcohol, butyl carbitol, longer chain alcohols, etc., and mixtures thereof. Examples of suitable longer chain alcohols include Cio, C12, C13, C14 and/or C15 monols, which may be used individually or as mixtures. Suitable monoethers include a hydrocarbyl residue (Z) in which the hydrocarbyl residue is a C4-C60, and preferably a C9-C30, alkyl, aryl or aralkyl group. The hydrocarbyl residue is typically derived from a monohydroxyl compound such as an alcohol or a phenol. Also suitable are monoethers derived from phenols substituted with C4-C15 alkyl groups such as, for example, nonylphenol, etc. Suitable epoxides can include, for example, ethylene oxide, propylene oxide, butylene oxide, styrene oxide, etc. and mixtures thereof. The epoxides can be polymerized with the low equivalent weight monofunctional starters using well- known techniques and a variety of catalysts, including alkali metals, alkali metal hydroxides and alkoxides, double metal cyanide complexes, and many more. Suitable monofunctional starters can also be made, for example, by first producing a diol or triol and then converting all but one of the remaining hydroxyl groups to an ether, an ester or other non-reactive group. Suitable monofunctional starters include those monols described in, for example, U.S. Patents 6,391 ,935 and 6,821 ,308, the disclosures of which are hereby incorporated by reference. Suitable polyoxyalkylene monols to be used as the monofunctional starter for (a) may contain up to 20% by weight, based on 100% by weight of the polyoxyalkylene monol, of copolymerized oxyethylene. [0025] The monol initiated oxyalkylene ether (a) may also be characterized in one embodiment as containing up to 20% by weight of copolymerized oxyethylene, based on the total weight of the monol initiated oxyalkylene ether (a). This weight percentage includes the initiator or starter and all of the added epoxide(s). These monol initiated oxyalkylene ethers (a) may contain less than or equal to 20% by weight, or less than or equal to 15% by weight, or less than or equal to 10% by weight, based on 100% by weight of the monol initiated oxyalkylene ether (a), of copolymerized oxyethylene. These monol initiated oxyalkylene ethers (a) may also contain more than 0%, or at least 2% or at least 5%, based on the total weight of the monol initiated oxyalkylene ether (a), of copolymerized oxyethylene. The amount of copolymerized oxyethylene present in the monol initiated oxyalkylene ethers (a) may vary between any combination of these upper and lower values, inclusive, such as, more than 0% to 20%, or 2% to 15%, or 5% to 10% by weight.

[0026] The monol initiated oxyalkylene ethers (a) can have virtually any desired arrangement of oxyalkylene units with the proviso that these contain less than or equal to 20% of copolymerized oxyethylene, based on the total weight of the monol initiated oxyalkylene ether (a). This weight percentage includes the initiator or starter and all of the added epoxide(s). Some examples of suitable monol initiated oxyalkylene ethers (a) include PO homopolymers, block EO-PO copolymers, random EO/PO copolymers, PO polymers that are “tipped” with EO or with a mixture of EO and PO are possible. These “tipped” PO polymers should use a mixture of EO and PO to achieve a particular oxyethylene content and/or a desired primary hydroxyl content, or any other desired configuration. The so-called PO homopolymers are suitable with the proviso that they satisfy the above described amounts of copolymerized oxyethylene.

[0027] In one embodiment, the monol initiated oxyalkylene ether (a) comprises an oxypropylene block next to the low equivalent weight monofunctional starter followed by a mixed oxypropylene and oxyethylene block at the end of the chain. In another embodiment, the oxyalkylene block at the end of the chain comprises copolymerized oxypropylene and copolymerized oxyethylene wherein the copolymerized oxyethylene content is 20% by weight or less, based on 100% by weight of the oxyalkylene block. [0028] Suitable polyether polyols for component (b) typically have a hydroxyl number of 20 to 240 mg KOH/g, and a nominal functionality of 2 to 8. These polyether polyols (b) may have hydroxyl numbers of at least 20 mg KOH/g, or at least 30 mg KOH/g, or at least 35 mg KOH/g. The polyether polyols (b) may also have hydroxyl numbers of less than or equal to 240 mg KOH/g, or of less than or equal to 170 mg KOH/g, or of less than or equal to 50 mg KOH/g. Suitable polyether polyols (b) may also have a hydroxyl number ranging between any combination of these upper and lower values, inclusive, such as 20 to 240 mg KOH/g, 30 to 170 mg KOH/g, or 35 to 50 mg KOH/g.

[0029] The average functionality of these polyether polyols (b) ranges from at least about 2, or from at least about 2.5. The average functionality is also typically about 8 or less, or about 6 or less. The average functionality of the polyether polyols (b) may range between any combination of these upper and lower values, inclusive, such as from about 2 to about 8, or from about 2.5 to about 6.

[0030] Suitable polyether polyols used as component (b) also contain at least 50% to about 99% by weight or less of copolymerized oxyethylene, based on 100% by weight of the polyether polyol (b). This weight percent includes the starter or initiator, and all of the added epoxide(s). These polyether polyols (b) may contain at least about 50%, or at least about 60% or at least about 70% by weight, of copolymerized oxyethylene, based on 100% by weight of the polyether polyol (b). These polyether polyols (b) may also contain about 99% or less, or about 90% or less, or about 85% or less of copolymerized oxyethylene, based on 100% by weight of the polyether polyol (b). Suitable polyether polyols (b) herein may contain any amount of copolymerized oxyethylene between the above disclosed values, inclusive, such as from about 50% to about 99%, from about 60% to about 90%, or from about 70% to about 85% by weight, of copolymerized oxyethylene.

[0031] Some examples of suitable polyether polyols for component (b) include those compounds which are conveniently made by reacting compounds having two or more active hydrogens (e.g., glycols, triols, tetrols, hexols, polyfunctional amines and other polyfunctional starters known to those in the art) with one or more equivalents of an epoxide. Examples of suitable starters for these polyether polyols (b) include low equivalent weight starters such as, for example, glycerin, propylene glycol, dipropylene glycol, ethylene glycol, trimethylolpropane, sucrose, sorbitol, tripropylene glycol and mixtures thereof.

[0032] Suitable epoxides for component (b) can include, for example, ethylene oxide, propylene oxide, butylene oxide, styrene oxide, etc., and mixtures thereof.

[0033] The polyether polyols for component (b) can have any desired arrangement of oxyalkylene units with the proviso that they contain at least 50% of copolymerized oxyethylene, based on the 100% by weight of the polyether polyol (b). Thus, the polyether polyols (b) can be EO homopolymers, block EO-PO copolymers, EO-capped polyoxypropylenes, random EO/PO copolymers, PO polymers that are “tipped” with a mixture of EO and PO to achieve the desired amount of copolymerized oxyethylene and/or a particular primary hydroxyl content, or any other desired configuration.

[0034] In one embodiment, the composition of the polyether polyol (b) contains a 100% oxyethylene block next to the low equivalent weight starter followed by a mixed block of oxyethylene and oxypropylene.

[0035] Suitable polyether polyols for component (c) typically have a hydroxyl number of 80 to 220 mg KOH/g, and a nominal functionality of 2. These polyether polyols (c) may have hydroxyl numbers of at least 80 mg KOH/g, or at least 100 mg KOH/g. The polyether polyols (c) may also have hydroxyl numbers of less than or equal to 220 mg KOH/g, or of less than or equal to 180 mg KOH/g. Suitable polyether polyols (c) may also have a hydroxyl number ranging between any combination of these upper and lower values, inclusive, such as 80 to 220 mg KOH/g, or 100 to 180 mg KOH/g. These polyether polyols (c) may be prepared from low equivalent weight starters such as, for example, propylene glycol, dipropylene glycol, ethylene glycol, tripropylene glycol, water, methyl-1 ,3-propanediol, and the like, and mixtures thereof.

[0036] Suitable polyether polyols for component (c) contain from 5 to 45% by weight of copolymerized oxyethylene. These polyether polyols (c) may contain at least 5%, or at least 10%, or at least 15%, of copolymerized oxyethylene, based on the total weight of the polyether polyol (c). These polyether polyols (c) may contain 45% or less, or 40% or less, or 35% or less of copolymerized oxyethylene, based on the total weight of the polyether polyol (c). The total weight of the polyether polyol (c) includes the starter or initiator, and all of the added epoxide(s). Suitable polyether polyols (c) herein may contain any amount of copolymerized oxyethylene between the above disclosed upper and lower values, inclusive, unless otherwise stated, such as 5% to 45% by weight, 10% to 40% by weight, or 15% to 35% by weight of copolymerized oxyethylene, based on the total weight of the polyether polyol (c).

[0037] These polyether polyols (c) can be block EO-PO copolymers, EO-capped polyoxypropylenes, random EO/PO copolymers, PO polymers that are “tipped” with a mixture of EO and PO to achieve the desired amount of copolymerized oxyethylene and/or a particular primary hydroxyl content, random EO/PO copolymers that vary the ratio of EO to PO along the chain to provide EO rich end groups or PO rich end groups or any other desired configuration.

[0038] In one embodiment, the polyether polyol (c) has a first mixed oxypropylene and oxyethylene block followed by a second mixed oxypropylene and oxyethylene block that has a higher copolymerized oxyethylene content compared to the first block. The second mixed oxypropylene and oxyethylene block has a weight ratio of oxyethylene that is at least 10% by weight more than the first oxypropylene and oxyethylene block based on the weight ratio of the mixed oxypropylene and oxyethylene blocks (i.e. if first block has a propylene oxide to ethylene oxide weight ratio of 90/10 then the second block has a weight ratio of ethylene oxide of at least 20% or 80/20).

[0039] Suitable polyether polyols for component (d) typically have a hydroxyl number of 80 to 220 mg KOH/g, a nominal functionality of greater than 2 to 8. These polyether polyols (d) may also have hydroxyl numbers of at least 80 mg KOH/g, or at least 100 mg KOH/g. The polyether polyols (d) may also have hydroxyl numbers of less than or equal to 220 mg KOH/g, or of less than or equal to 180 mg KOH/g. Suitable polyether polyols (d) may also have a hydroxyl number ranging between any combination of these upper and lower values, inclusive, such as 80 to 220 mg KOH/g, or 100 to 180 mg KOH/g. The polyether polyols (d) may also have a nominal functionality of greater than 2, or of at least 3. The nominal functionality of the polyether polyols (d) may also be less than or equal to 8, or less than or equal to 6. Suitable polyether polyols (d) may have a nominal functionality ranging between any combination of these upper and lower values, inclusive, such as greater than 2 to 8, or 3 to 6. These polyether polyols (d) may be prepared from low equivalent weight starters such as, for example, glycerin, trimethylolpropane, pentaerythritol, sucrose, sorbitol, and the like, and mixtures thereof. [0040] Suitable polyether polyols for component (d) contain from 5 to 45% by weight of copolymerized oxyethylene. These polyether polyols (d) may contain at least 5%, or at least 10%, or at least 15%, of copolymerized oxyethylene, based on the total weight of the polyether polyol (d). These polyether polyols (d) may contain 45% or less, or 40% or less, or 35% or less of copolymerized oxyethylene, based on the total weight of the polyether polyol (d). The total weight of the polyether polyol (d) includes the starter or initiator, and all of the added epoxide(s). Suitable polyether polyols (d) herein may contain any amount of copolymerized oxyethylene between the above disclosed upper and lower values, inclusive, unless otherwise stated, such as 5% to 45% by weight, 10% to 40% by weight, or 15% to 35% by weight of copolymerized oxyethylene, based on the total weight of the polyether polyol (d).

[0041] These polyether polyols (d) can be block EO-PO copolymers, EO-capped polyoxypropylenes, random EO/PO copolymers, PO polymers that are “tipped” with a mixture of EO and PO to achieve the desired amount of copolymerized oxyethylene and/or a particular primary hydroxyl content, random EO/PO copolymers that vary the ratio of EO to PO along the chain to provide EO rich end groups or PO rich end groups or any other desired configuration.

[0042] In one embodiment, the polyether polyol (d) has a first mixed oxypropylene and oxyethylene block followed by a second mixed oxypropylene and oxyethylene block that has a higher copolymerized oxyethylene content compared to the first block. The second mixed oxypropylene and oxyethylene block has a weight ratio of oxyethylene that is at least 10% by weight more than the first oxypropylene and oxyethylene block based on the weight ratio of the mixed oxypropylene and oxyethylene blocks (i.e. if first block has a propylene oxide to ethylene oxide weight ratio of 90/10 then the second block must have a weight ratio of ethylene oxide of at least 20% or 80/20).

[0043] The in-situ formed polyether polyol blend comprises 15% to 40% by weight of (a) the monol initiated oxyalkylene ether; 3 to 45% by weight of (b) the polyether polyol; 8 to 30% by weight of (c) the polyether polyol; and 20 to 60% by weight of (d) the polyether polyol, with the sum of the %’s by weight of (a), (b), (c) and (d) totaling 100% by weight of the in-situ formed polyether polyol blend. In a preferred embodiment, the in-situ formed polyether polyol blend comprises 15% to 35% by weight of (a) the monol initiated oxyalkylene ether; 3 to 45% by weight of (b) the polyether polyol; 8 to 25% by weight of (c) the polyether polyol; and 22 to 46% by weight of (d) the polyether polyol, with the sum of the %’s by weight of (a), (b), (c) and (d) totaling 100% by weight of the in-situ formed polyether polyol blend.

[0044] The phase stable in-situ formed polyether polyol blend comprises 15 to 40% by weight of (a) the monol initiated oxyalkylene ether; 3 to 10% by weight of (b) the polyether polyol; 15 to 30% by weight of (c) the polyether polyol; and 20 to 60% by weight of (d) the polyether polyol, with the sum of the %’s by weight of (a), (b), (c) and (d) totaling 100% by weight of the phase stable in-situ formed polyether polyol blend.

[0045] The process for preparing the in-situ formed polyether polyol blend having an overall functionality of 2 to 3 and an overall hydroxyl number of 40 to 220 mg KOH/g comprises

I) introducing into a reaction vessel a mixture comprising:

(1 ) an initially charged starter (Si) comprising a monofunctional compound having a hydroxyl number of less than or equal to 80 mg KOH/g, and

(2) a DMC (double metal cyanide) catalyst,

II) feeding

(1 ) an epoxide comprising propylene oxide and ethylene oxide in a weight ratio of 100:0 to 80:20, into the reaction vessel;

III) allowing the epoxide and the initially charged starter (Si) to react and continue polymerizing by feeding the epoxide until the equivalent weight of the monofunctional compound is increased by at least 10% by weight and reaches a value between 1 ,500 and 6,000;

IV) feeding (1 ) an epoxide mixture comprising propylene oxide and ethylene oxide in a weight ratio of 50:50 to 20:80, while continuously adding

(2) a continuously added starter (Sc) having a functionality of 2 to 8, and an equivalent weight of 28 to 400, into the reaction vessel;

V) completing addition of the continuously added starter (Sc);

VI) allowing the mixture to continue to polymerize in the reaction vessel thereby forming

(1 ) an intermediate in-situ formed polyether polyol blend having an overall hydroxyl number of 10 to 200 mg KOH/g, an overall functionality of greater than 1 to 3, and which comprises

(a) a monol initiated oxyalkylene ether having a hydroxyl number of less than or equal to 56 mg KOH/g, and containing less than 20% by weight of copolymerized oxyethylene, based on 100% by weight of the monol initiated oxyalkylene ether (a), and b) a polyether polyol having a hydroxyl number of 20 to 240 mg KOH/g, a nominal functionality of 2 to 8, and containing at least 50% by weight of copolymerized oxyethylene, based on 100% by weight of the polyether polyol (b),

VII) feeding

(1 ) an epoxide comprising propylene oxide and ethylene oxide in a weight ratio of 95:5 to 55:45, while continuously adding

(2) a continuously added starter (Sc) having a nominal functionality of 2 to 8, and an equivalent weight of 28 to 100, into the reaction vessel; VIII) completing addition of the continuously added starter (Sc) and epoxide thereby forming, in addition to monol initiated oxyalkylene ether (a) and polyether polyol

(b),

(c) a polyether polyol having a hydroxyl number of 80 to 220 mg KOH/g, a nominal functionality of 2, and containing 5 to 45% by weight of copolymerized oxyethylene, based on the total weight of the polyether polyol (c), and

(d) a polyether polyol having a hydroxyl number of 80 to 220 mg KOH/g, a nominal functionality of greater than 2 to 8, and containing 5 to 45% by weight of copolymerized oxyethylene, based on the total weight of the polyether polyol (d); wherein the in-situ formed polyether polyol blend comprises 15 to 40% by weight of (a) the monol initiated oxyalkylene ether, 3 to 45% by weight of the polyether polyol (b), 8 to 30% by weight of the polyether polyol (c), and 20 to 60% by weight of the polyether polyol (d), with the sum of the %’s by weight of (a), (b), (c) and (d) totaling 100% by weight of the in-situ formed polyether polyol blend.

[0046] In general, any epoxide polymerizable using double metal cyanide (DMC) catalysis can be used in the in-situ production of the polyether polyol blend comprising a monol initiated oxyalkylene ether (a) and the three polyether polyols (b), (c) and (d). Suitable epoxides include ethylene oxide, propylene oxide, butylene oxides (e.g., 1,2- butylene oxide, isobutylene oxide), styrene oxide, and the like, and mixtures thereof. Polymerization of epoxides using DMC catalysts and hydroxyl-containing starters results in polyether polyols, as is well understood in the art.

[0047] Other monomers that will copolymerize with an epoxide in the presence of a DMC catalyst may be included in the process of the invention to make other types of epoxide polymers. Some examples include epoxides copolymerize with oxetanes as described in U.S. Patent 3,404,109, the disclosure of which is herein incorporated by reference, to give polyethers, or with anhydrides to give polyesters or polyetheresters as described in U.S. Patents 5,145,883 and 3,538,043, the disclosures of which are herein incorporated by reference, or with carbon dioxide to form polyether carbonate polyols such as those described in U.S. Patents 4,826,887, 4,826,952, 4,826,953, 6,713,599, 7,977,501, 8,134,022, 8,324,419, 8,946,466 and 9,249,259, the disclosures of which are herein incorporated by reference, and U.S. Published Patent Application 2015/0232606. [0048] In accordance with this process, an initially charged starter (Si) is used, and the initially charged starter (Si) is different than the continuously added starter (Sc). The initially charged starter (Si) is comprised of, either totally or in large part, a compound having one active hydrogen per molecule that can serve as a site for epoxide addition, and having a hydroxyl number of less than or equal to 80 mg KOH/g, or of less than or equal to 56 mg KOH/g. The initially charged starter (Si) is the same as the monofunctional starters described above as suitable starters for the monol initiated oxyalkylene ether (a). These are formed by addition of multiple equivalents of epoxide to a low equivalent weight monofunctional starter such as, for example, methanol, ethanol, phenols, allyl alcohol, butyl carbitol, longer chain alcohols, etc., and mixtures thereof. Examples of suitable longer chain alcohols include Cio, C12, C13, C14 and/or C15 monols, which may be used individually or as mixtures. Suitable monoethers include a hydrocarbyl residue (Z) in which the hydrocarbyl residue is a C4-C60, and preferably a C9-C30, alkyl, aryl or aralkyl group. The hydrocarbyl residue is typically derived from a monohydroxyl compound such as an alcohol or a phenol. Also suitable are monoethers derived from phenols substituted with C4-C15 alkyl groups such as, for example, nonylphenol, etc. Suitable epoxides can include, for example, ethylene oxide, propylene oxide, butylene oxide, styrene oxide, etc. and mixtures thereof. The epoxides can be polymerized using well-known techniques and a variety of catalysts, including alkali metals, alkali metal hydroxides and alkoxides, double metal cyanide complexes, and many more. Suitable initially charged monofunctional starters (Si) can also be made, for example, by first producing a diol or triol and then converting all but one of the remaining hydroxyl groups to an ether, an ester or other non-reactive group.

[0049] One suitable class of polyether monol starters or initially charged starters (Si) includes polyoxypropylene monols having a hydroxyl number of less than or equal to 80 mg KOH/g, or of less than or equal to 56 mg KOH/g. These compounds facilitate DMC catalyzed addition of epoxide and provide suitable build ratios for the production of the in- situ formed polyether polyol blends herein. The polyoxypropylene monols used as the initially charged starter (Si) can be made using processes well known to the skilled artisan including processes defined in U.S. Patent 5,689,012, U.S. Patent 5,177,777, U.S. Patent 10,723,829, U.S. Patent 10,723,830 and U.S. Patent 10,738,155, the disclosures of which are herein incorporated by reference.

[0050] In the process of the present invention, the quantity of an initially charged starter (Si) used depends on many factors, including, for example, the reactor dimensions, the identity of the initially charged starter (Si), the equivalent weights of the initially charged starter (Si) and of the target product, the equivalent weight of the continuously added starter (Sc), and other factors.

[0051] Any DMC catalyst known in the art is suitable for use in the process of the present invention. These well-known catalysts are the reaction products of a water- soluble metal salt (e.g., zinc chloride) and a water-soluble metal cyanide salt (e.g., potassium hexacyanocobaltate). Preparation of suitable DMC catalysts is described in many references, including, for example, U.S. Patents 5,158,922, 4,477,589, 3,427,334, 3,941,849, 5,470,813, and 5,482,908, the disclosures of which are incorporated herein by reference. One suitable type of DMC catalysts is zinc hexacyanocobaltate.

[0052] The DMC catalyst includes an organic complexing agent. As disclosed in the preceding references, the complexing agent is needed for an active catalyst. Suitable complexing agents are water-soluble heteroatom-containing organic compounds that can complex with the DMC compound, as well as water-soluble aliphatic alcohols. An example of a suitable aliphatic alcohol is tert-butyl alcohol. The DMC catalyst may include, in addition to the organic complexing agent, a polyether, as is described in U.S. Patent 5,482,908, the disclosure of which is herein incorporated by reference.

[0053] Suitable DMC catalysts for use in the process are highly active catalysts such as those described in U.S. Patents 5,482,908 and 5,470,813, the disclosures of which are herein incorporated by reference. High activity allows the catalysts to be used at very low concentrations, and possibly at concentrations which are low enough to overcome any need to remove the catalyst from the in-situ formed polyether polyol blends.

[0054] The processes of the invention also requires continuously added starters (Sc) as described in detail herein. Conventional processes for making polyether polyols, including KOH-catalyzed and DMC-catalyzed processes, charge the catalyst and all the starter to be used to the reactor at the start of the polymerization, and then add the epoxide continuously. In the process of forming an in-situ formed polyether polyol blend suitable for the invention, the DMC catalyst and an initial monofunctional starter (or initially charged starter) (Si) are charged to the reactor followed by epoxide feed and polymerization until the monol reaches the desired equivalent weight. At this point, a first feed (i.e. as described in step IV)(2) above) of continuously added starter (Sc) is begun and it proceeds at a continuous controlled rate relative to the continuing epoxide feed until the addition of the first feed of continuously added starter (Sc) is completed. Epoxide feed is continued until the desired hydroxyl number of the first feed of continuously added starter (Sc) component is reached. The continuously added starter (Sc) may be mixed with the epoxide and added to the reactor, or it may be added to the reactor as a separate stream. It is also possible that DMC catalyst can be added continuously with the continuously added starter (Sc). In the process of the present invention to form an in-situ formed polyether polyol blend, a second feed (i.e. as described in step Vll)(2) above) of continuously added starter (Sc) can be started with the epoxide feed after the completion of the first feed of continuously added starter (Sc). The second feed of continuously added starter (Sc) can be the same starter compound as was used for the first feed of continuously added starter (Sc), or it can be a different starter compound. The epoxide and the epoxide composition can be the same during the second feed of continuously added starter (Sc) feed as during the first feed of continuously added starter (Sc) feed, or the epoxide and the epoxide composition can be different during the second feed of continuously added starter (Sc) feed as during the first feed of continuously added starter (Sc) feed. The skilled artisan knows and understands that the lowest equivalent weight substance preferably reacts with epoxide in the presence of DMC catalyst, hence the continuously added starter (Sc) will preferentially react with the epoxide that is continuously added with the continuously added starter (Sc). This is common ly known and referred to by one of ordinary skill in the art as “catch up kinetics”. This allows the in-situ production of different components of the polyether polyol blend while only minimally affecting the other, higher equivalent weight components. Catch up kinetics is described in “Chemistry and Technology of Polyols for Polyurethanes”, 2 ^nd Edition, Volume 1, 2016, M. lonescu, pages 189-190, the disclosure of which is herein incorporated by reference.

[0055] The continuously added starter (Sc) is typically a low equivalent weight starter or polyol or a blend of low equivalent weight starters or polyols. These low equivalent weight polyols have from 2 hydroxyl groups to 8 hydroxyl groups. It also may be beneficial to add more than one continuously added starter (Sc) having different functionalities either simultaneously or sequentially. The functionality of the continuously added starter (Sc) or multiple continuously added starters (Sc) should be chosen such that the average functionality of the resultant polyol is from 2 to 8, or from 2 to 3. These low equivalent weight polyols may have at least 2 hydroxyl groups. These low equivalent weight polyols may also have 8 hydroxyl groups or less, or 6 hydroxyl groups or less, or 3 hydroxyl groups or less. The low equivalent weight polyols used for the continuously added starter (Sc) may contain any number of hydroxyl groups which ranges between any combination of these upper and lower values, inclusive, such as from 2 hydroxyl groups to 8 hydroxyl groups, 2 hydroxyl groups to 6 hydroxyl groups, or 2 hydroxyl groups to 3 hydroxyl groups.

[0056] Suitable low equivalent weight polyols for the continuously added starter (Sc) have a nominal functionality of 2 to 8 and an equivalent weight of 28 to 400 mg KOH/g.

[0057] Examples of suitable low equivalent weight polyols to be used as the continuously added starter (Sc) include compounds such as, for example, glycerin, propylene glycol, dipropylene glycol, ethylene glycol, trimethylolpropane, sucrose, sorbitol, tripropylene glycol, low equivalent weight oxyalkylene polyether polyols, and mixtures thereof. Low equivalent weight oxyalkylene polyether polyols employed as the continuously added starter (Sc) are prepared by multiple epoxide addition to a low equivalent weight polyol or starters with two or more active hydrogens. The low equivalent weight oxyalkylene polyether polyol employed as the continuously added starter (Sc) can be polymerized using well-known techniques and a variety of catalysts, including alkali metals, alkali metal hydroxides and alkoxides, double metal cyanide complexes and many more. In one embodiment, the first feed of continuously added starter (Sc) in step IV)(2) above comprises a low equivalent weight oxyalkylene polyether polyol which may have an equivalent weight of 100 to 400, and the second feed of continuously added starter (Sc) in step Vll)(2) above may comprise propylene glycol and/or glycerin, or may have an equivalent weight of 28 to 100.

[0058] The continuously added starter (Sc) can also be other compounds having at least two active hydrogens per molecule, which are known to be suitable initiators for conventional DMC-catalyzed epoxide polymerizations, including compounds such as, for example, alcohols, thiols, aldehydes and ketones containing enolizable hydrogens, malonic esters, phenols, carboxylic acids and anhydrides, aromatic amines, acetylenes, and the like, and mixtures thereof. Examples of suitable active hydrogen-containing compounds appear in U.S. Patents 3,900,518, 3,941,849, and 4,472,560, the disclosures of which are incorporated herein by reference.

[0059] As described previously, a wide variety of epoxides can be employed in the current process. Propylene oxide and ethylene oxide are the most commonly used epoxides. A unique feature of the current process is that the compositions of the epoxide can be varied to control the composition of the monol initiated oxyalkylene ether (a) and polyether polyol constituents (b), (c) and (d) in the in-situ formed polyether polyol blend. For example, propylene oxide can be added alone during polymerization of the monol initiated oxyalkylene ether (a), prior to the start of the addition of the continuously added starter (Sc). After the first feed of continuously added starter (Sc) is started, a blend of ethylene oxide and propylene oxide can be fed to yield a high functionality polyether polyol comprised of a poly(oxyethylene-oxypropylene) copolymer. Because oxide addition via DMC catalysis occurs predominantly on the lower equivalent weight polyether polyol, the monol initiated oxyalkylene ether component can remain largely poly(oxypropylene). By reversing these sequences, the monol initiated oxyalkylene ether could be produced with higher poly(oxyethylene) content and the polyether polyol (from the first feed of continuously added starter (Sc)) could be predominantly poly(oxypropylene).

[0060] The epoxide composition may also be varied during the initial polymerization of the monol initiated oxyalkylene ether and/or at some point during and/or after the addition of the continuously added starter (Sc). This provides flexibility for controlling the distribution of oxyethylene or oxypropylene within the monol initiated oxyalkylene ether and the subsequent polyether polyols and allows some control of the primary versus secondary hydroxyl content of the monol initiated oxyalkylene ether and polyether polyols, and thus, the relative reactivity of the constituents in the final composition. In this way, it is possible to design the product to meet the reactivity and performance requirements of the intended applications such as viscoelastic polyurethane foams.

[0061] An example of the process to prepare an in-situ formed multifunctional polyether polyol blend is provided here. By way of example, the monol starter or initially charged starter (Si) may comprise a 1600 MW (35 OH#) monol inhibited with BHT made from the propoxylation of Neodol 25 (available from Shell) with a DMC catalyst. In a typical reaction to make the in-situ formed polyether polyol blend, the monol starter (or initially charged starter) (Si) is charged at room temperature followed by addition of the DMC catalyst as a dry powder. Alternatively, the monol starter or initially charged starter (Si) may be heated before addition to the reactor or it may be charged to a heated reactor. The DMC catalyst may also be added as a slurry in the monol starter or initially charged starter (Si). After charging the monol starter or initially charged starter (Si) and DMC catalyst, vacuum is pulled on the reactor contents. The reactor contents are heated to the reaction temperature. This may be followed by nitrogen stripping under vacuum. Vacuum and nitrogen stripping can occur before, during or after the reactor contents have reached the reaction temperature. After nitrogen stripping is stopped, the vacuum can be continued without nitrogen stripping. Before starting the oxide feed to the reactor, the reactor is blocked in under vacuum and can remain under vacuum for a given time to check for any leaks to the reactor. The DMC catalyst is then activated by adding a portion of propylene oxide or a mixture of propylene and ethylene oxide and allowing it to react. Prior to oxide addition, the reactor can be under vacuum or can be pressured up using nitrogen or other inert gas. After the DMC catalyst activation is complete as evidenced by a decrease in reactor pressure or by a specific temperature change, the oxide feed is restarted. The DMC catalyst can also be activated by starting the oxide feeds at a reduced rate and continuously adding the oxide feeds until the reactor temperature increases and the reactor pressure decreases and the reactor cooling system indicates that the reactor has switched from heating to cooling indicating that the catalyst is active and the reaction is proceeding. After detecting the activation either through the batch addition of oxide or the continuous feeding of oxide, the propylene and/or ethylene oxide feed rates are ramped up to the set point typically in 5 to 30 minutes. The typical reaction temperature for the DMC catalyzed reaction is 130 to 150°C with a mixture of propylene oxide and/or ethylene oxide. After the monol starter or initially charged starter (Si) has increased in molecular weight by at least 10% through the addition of propylene and/or ethylene oxide, a 240 OH# oxyethylene triol is continuously added along with a mixture of propylene oxide and ethylene oxide until a targeted hydroxyl number is reached. The ethylene oxide to propylene oxide during this step is greater than 50 weight % ethylene oxide based on the total propylene and ethylene oxide fed. The continuously added starter (Sc), i.e. a 240 OH# oxyethylene triol, may be started at the target feed rate or ramped to the target feed rate. Additionally the continuously added starter (Sc), i.e. 240 OH# oxyethylene triol, may be fed at a constant maximum feed rate or the feed rate may be varied during this step. After the target hydroxyl number is reached, the continuously added starter (Sc), i.e. 240 OH# oxyethylene triol, is stopped either at the target feed rate or by ramping down the feed rate. Propylene oxide and ethylene oxide at the same high EO ratio are continuously added after the continuously added starter (Sc) is stopped until a target hydroxyl number is reached. The feeding of alkylene oxide after the continuously added starter (Sc) stops is referred to as a non-CAOS cap. Alternatively, the non-CAOS cap may be eliminated and the continuously added starter (Sc), e.g. 240 OH# oxyethylene triol, continued until the target hydroxyl number is reached. After the continuously added starter (Sc) is stopped and the propylene oxide and ethylene oxide are fed to react away the continuously added starter (Sc), the propylene oxide and ethylene oxide can be fed continuously added at a different weight ratio that is higher in ethylene oxide until a target hydroxyl number is reached. This change in the propylene oxide and ethylene oxide weight ratio to a ratio higher in ethylene oxide may be accomplished by stopping the oxide feeds and restarting at the desired ratio or by simultaneously ramping down the propylene oxide feed and ramping up the ethylene oxide feed to the new peak feed rates and ratios. After the hydroxyl number of the 2 ^nd polyol (b) is reached, the ratio of ethylene oxide to propylene oxide is adjusted to a feed that is < 50 weight % EO based on the combined propylene oxide and ethylene oxide feeds and the continuously added starter (Sc), e.g. propylene glycol and/or glycerin, is started (i.e. a second feed of continuously added starter (Sc)). The continuously added starter (Sc), i.e. propylene glycol and/or glycerin feeds, may be started at the target feed rates or ramped to the target feed rates. The continuously added starter (Sc), i.e. propylene glycol and/or glycerin feeds, may be started simultaneously or at different times. Additionally the continuously added starter (Sc), i.e. propylene glycol and/or glycerin feeds, may be fed at a constant maximum feed rate or the feed rate of one or both may be varied during this step. After the target hydroxyl number is reached, the continuously added starter (Sc), i.e. propylene glycol and/or glycerin feeds, are stopped either at their target feed rates or by ramping down the feed rates. Propylene oxide and ethylene oxide are continuously added after the continuously added starter (Sc) are stopped until a target hydroxyl number is reached.

The feeding of alkylene oxide after the continuously added starter (Sc) stops is referred to as a non-CAOS cap. Alternatively, the non-CAOS cap may be eliminated and the continuously added starter (Sc), e.g. propylene glycol and/or glycerin feeds, continued until the target hydroxyl number is reached. After the continuously added starter (Sc) is stopped and the propylene oxide and ethylene oxide are fed to react away the continuously added starter (Sc), the propylene oxide and ethylene oxide are continuously added at a different weight ratio that is higher in ethylene oxide but still less than 50 weight % ethylene oxide based on the combined weight of propylene and ethylene oxide until a target hydroxyl number is reached. This change in the propylene oxide and ethylene oxide weight ratio from a ratio low in ethylene oxide to one that is higher in ethylene oxide may be accomplished by stopping the oxide feeds and restarting at the desired ratio or by simultaneously ramping down the propylene oxide feed and ramping up the ethylene oxide feed to the new peak feed rates and ratios. The propylene oxide and ethylene oxide feed rates may be stopped directly or ramped down to zero. This in- situ formed multifunctional polyether polyol blend can have an overall functionality of 2 to 3 and an overall hydroxyl number of 40 to 220 mg KOH/g. At the conclusion of the oxide feeds, all feed lines are blown out with nitrogen into the reactor and the reactor contents are held at the reaction temperature (cooked-out) until the reactor pressure levels off.

After this the product is stripped under vacuum simultaneously or continuously with nitrogen sparging and/or steam in one or more steps. The in-situ formed polyether polyol is then cooled typically to 80 to 100°C and one or more antioxidants are added followed by mixing. The product is then cooled to 40 to 80°C and discharged from the reactor. Antioxidant addition can occur at different temperatures and the final in-situ formed polyether polyol can be discharged from the reactor at different temperatures. The total alkylene oxide addition time can range from 30 minutes to 12 hours depending on the mixing of the reaction system and the heat removal capability of the reaction system. The alkylene oxide feed rates can remain constant during the feeding of alkylene oxide or one or more of the alkylene oxide feed rates can vary during the course of the alkylene oxide feed to provide improved reaction conditions (i.e. , mixing, heat removal, etc) or improved product quality or optimized composition (i.e., increased EO composition by increasing the EO feed rate and decreasing or holding constant the PO feed rate).

[0062] The process for the production of a viscoelastic polyurethane foam comprises reacting (A) a diisocyanate and/or a polyisocyanate component, with (B) an isocyanate- reactive component comprising (1) the in-situ formed polyether polyol blend having an overall functionality of 2 to 3 and an overall hydroxyl number of 40 to 220 mg KOH/g which is described herein, in the presence of (C) a blowing agent, (D) a catalyst, and (E) a surfactant.

[0063] Suitable diisocyanates and polyisocyanates to be used as component (A) in the viscoelastic foams herein and the process of making these foams include, for example, isocyanate-functional compounds which contain two or more free NCO groups per molecule and are known to be useful for preparing flexible polyurethane foam. Suitable isocyanate-functional compounds include aromatic, aliphatic, and cycloaliphatic di- and/or polyisocyanates. Some examples include toluene diisocyanates (TDI), diphenylmethane diisocyanates (MDI), naphthalene diisocyanates, isophorone diisocyanate, hexamethylene diisocyanates (HDI), polymeric MDIs, and polyisocyanates modified with carbodiimide, ester, urea, urethane, allophanate, isocyanurate, biuret, or other functionalities, and the like, and mixtures thereof. Suitable polyisocyanates include toluene diisocyanate (TDI, which is usually a mixture of 2,4- and 2,6-isomers), diphenylmethane diisocyanate (MDI which is usually a mixture of the 2,2’-, the 2,4’- and the 4,4’-isomers), and various mixtures thereof. In one embodiment, the isocyanate-functional compound comprises toluene diisocyanate, preferably a mixture of 2,4- and 2,6-isomers .

[0064] The isocyanate-reactive component (B) comprises the in-situ formed polyether polyol blend (1) described herein which has an overall hydroxyl number of 40 to 220 mg KOH/g and an overall functionality of 2 to 3. The in-situ formed polyether polyol blend may have a hydroxyl number ranging between any combination of these upper and lower values, inclusive, such as 50 to 200 mg KOH/g.

[0065] In the isocyanate-reactive component (B), the in-situ formed polyether polyol blend (1 ) also typically has an overall functionality of 2 to 3.

[0066] The composition of the in-situ formed polyether polyol blend (1) is as described hereinabove. The composition of the phase stable in-situ formed polyether polyol blend is also as described hereinabove.

[0067] In addition to the in-situ formed polyether polyol blend (1), the isocyanate- reactive component (B) for the process of preparing the viscoelastic flexible foams may additionally comprise a conventional polyether polyol, a polyester polyol, a polyether carbonate polyol, a polyetherester polyol, polymer polyols, amine-terminated polyethers, polythioethers, polyacetals, polycarbonates, etc., as well as various low equivalent weight chain extenders and/or crosslinking agents, both of which may contain hydroxyl groups and/or amine groups capable of reacting with the isocyanate groups of the isocyanate component. [0068] The in-situ formed polyether polyol blend (1 ) essentially corresponds to the in-situ formed polyether polyol blend described herein above, and is characterized by the same overall hydroxyl numbers and average functionalities.

[0069] In addition, in the process of preparing the viscoelastic flexible polyurethane foam, the isocyanate-reactive component (B) which comprises (1) the in-situ formed polyether polyol blend described above may additionally comprise (2) a filled polyol.

[0070] Filled polyols are also known as polymer polyols. Suitable filled polyols include, for example, (i) styrene/acrylonitrile (SAN) polymer polyols, (ii) polyisocyanate polyaddition (PIPA) polyols which are dispersions of polyurethanes formed by the in-situ reaction of an isocyanate and an alkanolamine, (iii) polyhydrazodicarbonamide dispersion polyols (also known as PHD polyols), and (iv) mixtures thereof.

[0071] Suitable (i) SAN polymer polyols herein are prepared by free radical polymerization of monomers (i.e. styrene and acrylonitrile) in a polyol carrier (or base polyol) to produce a free radical polymer dispersed in the polyol carrier (or base polyol). Conventionally, the solids content of SAN polymer polyols is from 5% to 60% by weight of solids, based on the total weight of the SAN polymer polyol composition. The solids content may be at least 5%, or at least 10% by weight of solids, based on the total weight of the SAN polymer polyol composition. The solids content may also be 60% by weight or less, or 50% by weight or less, based on the total weight of the SAN polymer polyol composition. The amount of solids content may range between any combination of these upper and lower values, inclusive, such as 5% to 60%, or 10% to 50% by weight of solids, based on the total weight of the SAN polymer polyol composition.

[0072] Examples of suitable SAN polymer polyols to be used as component (B)(2) herein include those SAN polymer polyols disclosed in, for example, but are not limited to,

U S. Patents 5,321,077, 5,324,774, 5,364,906, 5,358,984, 5,453,469, 5,488,085, 5,496, 894, 5,554,662, 5,594,066, 5,814,699, 5,824,712, 5,916,994, 5,995,534, 5,990,185, 6,117,937, 6,455,603, 6,472,447, 6,624,209, 6,713,599, 6,756,414, 7,179,882,

7,759,423, etc., the disclosures of which are hereby incorporated by reference.

[0073] Suitable polyisocyanate polyaddition (PIPA) polyols contain polyurethane particles dispersed in a polyol carrier (i.e. base polyol). The polyurethane particles in PIPA polyols are formed in-situ by the reaction of an isocyanate with an alkanolamine (e.g., triethanolamine). The solids content of the PIPA polyols may typically range from 5% to 60% by weight, based on the total weight of the PIPA composition. The solids content may be at least 5%, or at least 10% by weight of solids, based on the total weight of the PIPA composition. The solids content may also be 60% by weight of less, or 50% by weight or less, based on the total weight of the PIPA composition. The amount of solids content may range between any combination of these upper and lower values, inclusive, such as 5% to 60%, or 10% to 50% by weight of solids, based on the total weight of the PIPA composition.

[0074] Examples of suitable PIPA polyols can be found in, for example, U.S. Patents 4,374,209 and 5,292,778, the disclosures of which are herein incorporated by reference.

[0075] Suitable polyhydrazodicabonamide polyols (which are also commonly referred to as PHD polyols or PHD dispersion polyols) to be used include, for example, those compounds which are typically prepared by the in-situ polymerization of an isocyanate mixture with an amine group containing compound such as, a diamine and/or a hydrazine, in a base polyol. Suitable base polyols typically comprise polyether polyols and polyoxyalkylene polyols. Methods for preparing PHD polymer polyols are described in, for example, U.S. Patents 4,089,835 and 4,260,530, the disclosures of which are hereby incorporated by reference.

[0076] PHD polyols typically have solids contents within the range of 3 to 30 weight %, based on the total weight of the PHD polyol. The solids content of the PHD polyols may be at least 3%, or at least 5% by weight, based on the total weight of the PHD polyol. The solids content of the PHD polyols may also be 30% or less, or 25% by weight or less, based on the total weight of the PHD polyol. The PHD polyols may have a solids content that ranges between any combination of these upper and lower values, inclusive, such as 3% to 30% by weight, or 5 to 25% by weight, based on the total weight of the PHD polyol. [0077] As previously stated, PHD polyols are typically prepared by the in-situ polymerization of an isocyanate mixture in a polyol. More specifically, the isocyanate mixture typically comprises 80 parts by weight, based on the total weight of the isocyanate mixture, of 2,4-toluene diisocyanate, and 20 parts by weight, based on the total weight of the isocyanate mixture, of 2,6-toluene diisocyanate.

[0078] Suitable amine group containing compounds to be polymerized with the isocyanate compound include in preparing the PHD polyols, for example, compounds such as polyamines, hydrazines, hydrazides, ammonia or mixtures of ammonia and/or urea and formaldehyde.

[0079] PHD polymer modified polyols are typically prepared by the in-situ polymerization of an isocyanate mixture with a diamine and/or hydrazine in a base polyol, preferably, a polyether polyol. Methods for preparing PHD polymer polyols are described in, for example, United States Patents 4,089,835, 4,260,530 and 4,324,715, the disclosures of which are hereby incorporated by reference.

[0080] In one embodiment, a foam modifier or foam processing aid is added to the formulation to enhance processing and help stabilize the viscoelastic flexible foam against cold flow and/or dishing by providing dimensional stability against deformation and reduced settling of the viscoelastic flexible foam. These processing aids or modifiers are typically chain extenders and/or cross-linking agents.

[0081] In addition, the foam modifiers or processing aids may have a hydroxyl number of at least 300 mg KOH/g or of at least 600 mg KOH/g.

[0082] Suitable blowing agents (C) for the present invention include, for example chemical blowing agents, i.e. isocyanate reactive agents that generate blowing gases, such as for example water and formic acid and physical blowing agents such as acetone, carbon dioxide, chlorofluorocarbons, highly fluorinated and/or perfluorinated hydrocarbons, chlorinated hydrocarbons, aliphatic and/or cycloaliphatic hydrocarbons such as propane, butane, pentane, hexane, etc., or acetals such as methylal. These physical blowing agents are usually added to the polyol component of the system. However, they can also be added in the isocyanate component or as a combination of both the polyol component and the isocyanate component. It is also possible to use them together with highly fluorinated and/or perfluorinated hydrocarbons, in the form of an emulsion of the polyol component. If emulsifiers are used, they are usually oligomeric acrylates which contain polyoxyalkylene and fluoroalkane radicals bonded as side groups and have a fluorine content of 5 to 30% by weight. Such products are sufficiently well known from plastics chemistry, and are described in U.S. Patent 4,972,002, the disclosure of which is herein incorporated by reference.

[0083] The amount of blowing agent or blowing agent mixture used may range from 0.5 to 20% by weight, based on 100% by weight of (B) the isocyanate-reactive component. As used herein with respect to the amount of blowing agent, the isocyanate-reactive component includes (1) the in-situ formed polyether polyol blend having an overall functionality of 2 to 3 and an overall hydroxyl number of 40 to 220 mg KOH/g as described herein. The blowing agent may be present in any amount ranging between any combination of these upper and lower above values, inclusive, such as 0.75% to 10% by weight, based on 100% by weight of component (B).

[0084] When water is the blowing agent, the amount of water typically present can range from at least 0.5 to 10%, based on 100% by weight of component (B) the isocyanate- reactive component. Water as a blowing agent may be present in any amount ranging between any combination of these upper and lower values, inclusive, such as 0.75% to 7% by weight, based on 100% by weight of component (B). The addition of water can be effected in combination with the use of the other blowing agents described herein. In accordance with the present invention, water is the preferred blowing agent. In another embodiment, the blowing agent may comprise water along with pressurized carbon dioxide that is dispersed in the polyol or resin blend and frothed by passing through a pressure let down device such as employed, for example, in the Henecke Novaflex, CarDio (Cannon Viking Limited) and Beamech (CO2) machines, which are known by those skilled in the art. [0085] The viscoelastic flexible foam is produced in the presence of a surfactant, which helps to stabilize the viscoelastic flexible foam until it cures. Suitable surfactants are those well known in the polyurethane industry. A wide variety of organosilicone surfactants are commercially available. Examples of suitable surfactants are Niax L-620 surfactant, a product of Momentive Performance Materials, and Tegostab B8244, a product of Evonik- Goldschmidt. Many other silicone surfactants known to those in the art may be substituted for these suitable silicones. The surfactant is typically used in an amount within the range of at least 0.1 to 4 parts, based on 100% by weight of component (B). The amount of surfactant may range between any combination of these upper and lower values, inclusive, such as 0.2 to 3 parts, based on 100% by weight of component (B).

[0086] At least one polyurethane catalyst is required to catalyze the reactions of the isocyanate-reactive components and water with the polyisocyanate. It is common to use both an organoamine and an organotin compound for this purpose. Suitable polyurethane catalysts are well known in the art; an extensive list appears in U.S. Patent 5,011 ,908, the disclosure of which is herein incorporated by reference. Suitable organotin catalysts include tin salts and dialkyltin salts of carboxylic acids. Examples include stannous octoate, dibutyltin dilaurate, dibutyltin diacetate, stannous oleate, and the like. Stannous octoate is particularly preferred. Preferred organoamine catalysts are tertiary amines such as trimethylamine, triethylamine, triethylenediamine, bis(2,2'-dimethyl-amino)ethyl ether, N-ethylmorpholine, diethylenetriamine, and the like.

[0087] The polyurethane catalysts are typically used in an amount within the range of 0.01 to 3 parts, based on 100% by weight of component (B). The polyurethane catalysts may be present in amounts of at least 0.01 , or at least 0.1 parts, based on 100% by weight of component (B). The polyurethane catalysts may be present in amounts of 3 parts or less, or 2 parts or less based on 100% by weight of component (B). The polyurethane catalysts may be present in any amount ranging between any combination of these upper and lower values, inclusive, such as 0.1 to 2 parts, based on 100% by weight of component (B).

[0088] Flame retardants, antioxidants, pigments, dyes, liquid and solid fillers, and many other commercial additives can also be included in the viscoelastic flexible foams in conventional amounts.

[0089] The viscoelastic flexible foams are prepared using methods that are well known in the industry. These methods may include continuous or discontinuous free-rise slabstock foam processes and molded foam processes. In a typical slabstock process, the isocyanate is continuously mixed together with the other formulation chemicals by passing through a mixing head and then into a trough which overflows onto a moving conveyor.

[0090] Alternatively, the reacting mixture is deposited directly onto the moving conveyor. In another embodiment, high pressure liquid carbon dioxide is fed into one or more of the formulation components, typically the polyol, entering into the mixing head and the resin blend is passed through a frothing device where the pressure is let down and the resultant froth is deposited onto the conveyor. The viscoelastic flexible foam expands and rises as it moves down the conveyor to form a continuous foam slab that is cut into blocks or buns of the desired length for curing and storage. After curing for one or more days, these foam buns can be cut into the desired shapes for the end-use applications. In the discontinuous process, the reactants are quickly mixed together through a head or in a large mixing chamber. The reaction mixture is then deposited into a large box or other suitable container where foam expansion occurs to form a bun of the lateral dimensions of the container.

[0091] A typical molded viscoelastic flexible foam process usually employs a one-shot approach in which a specific amount of the isocyanate stream (the "A" side) is rapidly combined and mixed with a specific amount of the remaining formulation components (the "B" side). An additional stream may be employed to bring in one or more specific components not included with the "B" side stream. The mixture is quickly deposited into a mold that is then closed. The viscoelastic flexible foam expands to fill the mold and produce a part with the shape and dimensions of the mold.

[0092] Although less preferred, an isocyanate-terminated prepolymer approach to making the viscoelastic flexible foams can also be used. In this approach, a significant portion of the isocyanate-reactive mixture is reacted with the polyisocyanate, and the resulting isocyanate-terminated prepolymer is then reacted with the remaining components.

[0093] As used and referred to throughout the specification, air flow is measured in accordance with the NOPCO test procedure described by R.E. Jones and G. Fesman,

“Journal of Cellular Plastics,” January, 1965,Vol. No. 1, pp. 200-216, the dislcosure of which is herein incorporated by reference, using a Amscor Model 1377 automated foam porosity tester. A 2 inch x 2 inch x 1 inch piece of foam is cut from near the center of the test specimens which itself is cut from the foam blocks after production. Air flow, expressed as standard cubic feet per minute (i.e. scfpm), is measured through the 1 inch thickness at a pressure differential of 0.5 inches of water less than atmospheric pressure. The air flow is in the direction of rise of the foam. [0094] The test used to define foam recovery rate from deformation is the 95% height recovery time as described in ASTM D3574-17. A recovery rate of less than 3 seconds, indicates a fast recovering foam such as observed for resilient foam types. A recovery rate of greater than or equal to 3 seconds is indicative of a slow recovery foam often referred to as “viscoelastic” or “memory” foam.

[0095] Other viscoelastic flexible foam physical properties reported in the examples are measured per the standard procedures described in ASTM D3574-17 having the title “Standard Test Methods for Flexible Cellular Materials — Slab, Bonded, and Molded Urethane Foams”.

[0096] Commercial production of viscoelastic flexible foams involves mixing together a suitable polyisocyanate, and an isocyanate-reactive component which comprises the in-situ formed polyether polyol blend described above, in the presence of a blowing agent, a surfactant, a catalyst, and optionally, various other compounds which are known in the field of polyurethane chemistry to be suitable for preparing viscoelastic flexible foams.

[0097]

[0098] The following examples further illustrate details for the process of this invention. The invention, which is set forth in the foregoing disclosure, is not to be limited either in spirit or scope by these examples. Those skilled in the art will readily understand that known variations of the conditions of the following procedures can be used. Unless otherwise noted, all temperatures are degrees Celsius and all parts and percentages are parts by weight and percentages by weight, respectively.

EXAMPLES

[0099] Test Methods: The physical properties reported herein were measured per the standard procedures described in ASTM D3574-17 having the title “Standard Test Methods for Flexible Cellular Materials — Slab, Bonded, and Molded Urethane Foams” unless otherwise stated.

[0100] Flydroxyl Numbers: The hydroxyl numbers were determined in accordance with ASTM D-4274-11 , and are reported in mg KOFI/g polyol.

[0101] As used herein, “pphp” represents parts per hundred parts polyol. [0102] The following materials were used in the working examples:

Polvether Polyol A: A trifunctional polyether polyol prepared by alkoxylating glycerin with a KOH catalyst according to the procedure described in U.S. Patents 8,865,945 B2 and 9,169,185 B2. 2295 g of glycerin containing about 0.22% of a KOH catalyst solution were alkoxylated with 14499 g of ethylene oxide. The ethylene oxide was charged at a feed rate of 42 g/min. The resulting crude polyether polyol was over neutralized by charging a molar excess of a 12 weight % sulfuric acid solution. The resulting polyether polyol had a hydroxyl number of about 246 mg KOH/g and contained about 85% ethylene oxide, based on the weight of the polyether polyol.

Polvether Polyol B: An in-situ formed multifunctional polyether polyol prepared by alkoxylating a monol, diol, and triol with a DMC catalyst following the procedure described in U.S Patent 6,491 ,846. The starter comprised a 1600 MW (35 OH#) monol made from the propoxylation of Neodol 25. 3390 g of this 1600 MW monol were alkoxylated with 3287 g of a mixture of propylene oxide and ethylene oxide in a weight ratio of 82/18 to a hydroxyl number of about 17.8 mg KOH/g. The alkoxide mixture was charged at a combined feed rate of 60.26 g/min. The resulting 17.8 hydroxyl number monol contained a total of about 8.5 weight % ethylene oxide based on the total weight of the monol.

Next, 1107 g of a mixture of glycerin and propylene glycol in a 62.3 to 37.7 weight% ratio was continuously added at a combined feed rate of 7.91 g/min along with 8437 g of a mixture of propylene oxide and ethylene oxide in a weight ratio of 82/18 until a hydroxyl number of about 123 mg KOH/g was reached for the intermediate in-situ formed polyether polyol blend. The alkoxide mixture was charged at a combined feed rate of 60.26 g/min. At this point, the propylene glycol and glycerin feeds were stopped and an additional 441 g of the propylene oxide and ethylene oxide mixture were continuously added until a hydroxyl number of about 120 mg KOH/g was reached. At this point the reactor contained a mixture of the previously mentioned 17.8 hydroxyl number monol, a diol intermediate with a hydroxyl number of 187 mg KOH/g and a triol intermediate with a hydroxyl number of 187 mg KOH/g. Then, 3333 g of a mixture of propylene oxide and ethylene oxide were continuously added in a weight ratio of 55/45 at a combined feed rate of 60.26 g/min until the hydroxyl number of the diol and triol components reached about 140 mg KOH/g. The diol and triol components each contained a total of about 23 weight % ethylene oxide, based on the total weight of the individual diol and triol components. This in-situ formed polyether polyol blend contained 33 weight % monol, 22 weight % diol and 45 weight % triol. The in-situ formed polyether polyol blend had an overall functionality of about 2.4, total ethylene oxide content of about 18.5 weight %, based on the total weight of the in-situ formed polyether polyol blend and an overall hydroxyl number of about 100 mg KOH/g.

Polvether Polyol C: An in-situ formed multifunctional polyether polyol blend prepared with a DMC catalyst as follows. The starter comprised a 1600 MW (35 OH#) monol made from the propoxylation of Neodol 25. 3122 g of this 1600 MW monol (Si) were alkoxylated with 3017 g of a mixture of propylene oxide and ethylene oxide in a weight ratio of 82/18 to a hydroxyl number of about 17.8 mg KOH/g. The alkoxide mixture was charged at a combined feed rate of 60.83 g/min. The resulting 17.8 hydroxyl number monol (a) contained a total of about 8.5 weight% ethylene oxide based on the total weight of (a). Next 210 g of Polyol A (Sc) was continuously added at a feed rate of 7.62 g/min along with 1190 g of a mixture of propylene oxide and ethylene oxide in a weight ratio of 28/72 until a hydroxyl number of about 21.4 mg KOH/g was reached for the intermediate in-situ formed polyether polyol blend.

The resulting 37 hydroxyl number triol (b) contained a total of about 74 weight % ethylene oxide based on the weight of (b). Next, 1031 g of a mixture of glycerin and propylene glycol in a 62.3 to 37.7 wt% ratio (Sc) was continuously added at a combined feed rate of 8.02 g/min along with 7819 g of a mixture of propylene oxide and ethylene oxide in a weight ratio of 82/18 until a hydroxyl number of about 116 mg KOH/g was reached for the intermediate in-situ formed polyether polyol blend. The alkoxide mixture was charged at a combined feed rate of 60.83 g/min. At this point, the propylene glycol and glycerin feeds were stopped and an additional 512 g of the propylene oxide and ethylene oxide mixture were continuously added until a hydroxyl number of about 113 mg KOH/g was reached for the intermediate in- situ formed polyether polyol blend. At this point the reactor contained a mixture of the previously mentioned 17.8 hydroxyl number monol (a) and 37 hydroxyl number triol (b), a diol intermediate with a hydroxyl number of 187 mg KOH/g and a triol intermediate with a hydroxyl number of 187 mg KOH/g. Then, 3100 g of a mixture of propylene oxide and ethylene oxide were continuously added in a weight ratio of 55/45 at a combined feed rate of 60.83 g/min until the hydroxyl number of the diol (c) and triol (d) components reached about 140 mg KOH/g. The diol (c) and triol (d) components each contained a total of about 23 weight % ethylene oxide based on the total weight of the individual diol or triol component. This in-situ formed polyether polyol blend contained 30.7 weight % monol (a), 7 weight % of a 37 hydroxyl number triol (b), 20.5 weight % of a 140 hydroxyl number diol (c) and 41.8 weight % of a 140 hydroxyl number triol (d). The in-situ formed polyether polyol blend had an overall functionality of about 2.4, total ethylene oxide content of about 22.4 weight % based on the total weight of the in-situ formed polyether polyol blend and an overall hydroxyl number of about 95.4 mg KOH/g.

Polyether Polyol D: An in-situ formed multifunctional polyether polyol blend prepared with a DMC catalyst as follows. The starter comprised a 1600 MW (35 OH#) monol made from the propoxylation of Neodol 25. 3122 g of this 1600 MW monol (Si) were alkoxylated with 3017 g of a mixture of propylene oxide and ethylene oxide in a weight ratio of 82/18 to a hydroxyl number of about 17.8 mg KOH/g. The alkoxide mixture was charged at a combined feed rate of 60.83 g/min. The resulting 17.8 hydroxyl number monol (a) contained a total of about 8.5 weight % ethylene oxide based on the total weight of (a). Next 210 g of Polyol A (Sc) were continuously added at a feed rate of 7.62 g/min along with 1190 g of a mixture of propylene oxide and ethylene oxide in a weight ratio of 28/72 until the hydroxyl number of the intermediate in- situ formed polyether polyol blend reached about 21.4 mg KOH/g.

The resulting 37 hydroxyl number triol (b) contained a total of about 74 weight % ethylene oxide based on the total weight of (b). Next, 1031 g of a mixture of glycerin and propylene glycol in a 62.3 to 37.7 weight% ratio (Sc) was continuously added at a combined feed rate of 8.02 g/min along with 7819 g of a mixture of propylene oxide and ethylene oxide in a weight ratio of 68.5/31.5 until a hydroxyl number of about 116 mg KOH/g was reached for the intermediate in-situ formed polyether polyol blend. The alkoxide mixture was charged at a combined feed rate of 60.83 g/min. Then, the propylene glycol and glycerin feeds were stopped and an additional 512 g of the propylene oxide and ethylene oxide mixture were continuously added until a hydroxyl number of about 113 mg KOH/g was reached for the intermediate in-situ formed polyether polyol blend. At this point the reactor contained a mixture of the previously mentioned 17.8 hydroxyl number monol (a) and 37 hydroxyl number triol (b), a diol intermediate with a hydroxyl number of 187 mg KOH/g and a triol intermediate with a hydroxyl number of 187 mg KOH/g. Then 3100 g of a mixture of propylene oxide and ethylene oxide were continuously added in a weight ratio of 55/45 at a combined feed rate of 60.83 g/min until the hydroxyl number of the diol (c) and triol (d) components reached about 140 mg KOH/g. The diol (c) and triol (d) components each contained a total of about 29 weight % ethylene oxide based on the total weight of the individual diol (c) or triol component (d). This in-situ formed polyether polyol blend contained 30.7 weight % monol (a), 7 weight % of a 37 hydroxyl number triol (b), 20.5 weight % of a 140 hydroxyl number diol (c) and 41.8 weight % of a 140 hydroxyl number triol (d). The in-situ formed polyether polyol blend had an overall functionality of about 2.4, a total ethylene oxide content of about 26% based on the total weight of the in-situ formed polyether polyol blend and an overall hydroxyl number of about 95.4 mg KOH/g.

Polyether Polyol E: An in-situ formed multifunctional polyether polyol blend prepared with a DMC catalyst as follows. The starter comprised a 1600 MW (35 OH#) monol made from the propoxylation of Neodol 25. 3017 g of this 1600 MW monol (Si) were alkoxylated with 2926 g of a mixture of propylene oxide and ethylene oxide in a weight ratio of 82/18 to a hydroxyl number of about 17.8 mg KOH/g. The alkoxide mixture was charged at a combined feed rate of 61.03 g/min. The resulting 17.8 hydroxyl number monol (a) contained a total of about 8.5 weight % ethylene oxide based on the total weight of (a). Next 301 g of Polyol A (Sc) were continuously added at a feed rate of 7.28 g/min along with 1699 g of a mixture of propylene oxide and ethylene oxide in a weight ratio of 28/72 until a hydroxyl number of about 22.6 mg KOH/g was reached for the intermediate in-situ formed polyether polyol blend. The alkoxide mixture was charged at a combined feed rate of 61.03 g/min. The resulting 37 hydroxyl number triol (b) contained a total of about 74 % ethylene oxide based on the total weight of (b). Next, 998 g of a mixture of glycerin and propylene glycol in a 62.3 to 37.7 weight% ratio (Sc) was continuously added at a combined feed rate of 8.16 g/min along with 7463 g of a mixture of propylene oxide and ethylene oxide in a weight ratio of 82/18 until a hydroxyl number of about 114 mg KOH/g was reached for the intermediate in-situ formed polyether polyol blend. The alkoxide mixture was charged at a combined feed rate of 61.03 g/min. Then, the propylene glycol and glycerin feeds were stopped and an additional 493 g of the propylene oxide and ethylene oxide mixture were continuously added until a hydroxyl number of about 111 mg KOH/g was reached for the intermediate in-situ formed polyether polyol blend. At this point the reactor contained a mixture of the previously mentioned 17.8 hydroxyl number monol (a) and 37 hydroxyl number triol (b), a diol intermediate with a hydroxyl number of 187 mg KOH/g and a triol intermediate with a hydroxyl number of 187 mg KOH/g. Next 3015 g of a mixture of propylene oxide and ethylene oxide were continuously added in a weight ratio of 55/45 at a combined feed rate of 61.03 g/min until the hydroxyl number of the diol (c) and triol (d) components reached about 140 mg KOH/g. The diol (c) and triol (d) components each contained a total of about 23 weight % ethylene oxide based on the total weight of the individual diol (c) or triol (d) component. This in-situ formed polyether polyol blend contained 29.7 weight % monol (a), 10 weight % of a 37 hydroxyl number triol (b), 19.8 weight % of a 140 hydroxyl number diol (c) and 40.5 weight % of a 140 hydroxyl number triol (d). The in- situ formed polyether polyol blend had an overall functionality of about 2.4, total ethylene oxide content of about 24 weight % based on the total weight of the in-situ formed polyether polyol blend and an overall hydroxyl number of about 93.6 mg KOH/g.

Polvether Polyol F: An in-situ formed multifunctional polyether polyol blend prepared with a DMC catalyst as follows. The starter comprised a 1600 MW (35 OH#) monol made from the propoxylation of Neodol 25. 2882 g of this 1600 MW monol (Si) were alkoxylated with 2910 g of a mixture of propylene oxide and ethylene oxide in a weight ratio of 82/18 to a hydroxyl number of about 17.8 mg KOH/g. The alkoxide mixture was charged at a combined feed rate of 61.28 g/min. The resulting 17.8 hydroxyl number monol (a) contained a total of 8.5 weight % ethylene oxide based on the total weight of (a). Next 422 g of Polyol A (Sc) were continuously added at a feed rate of 8.03 g/min along with 2378 g of a mixture of propylene oxide and ethylene oxide in a weight ratio of 28/72 until a hydroxyl number of about 24 mg KOH/g was reached for the intermediate in-situ formed polyether polyol blend. The alkoxide mixture was charged at a combined feed rate of 61.28 g/min. The resulting 37 hydroxyl number triol (b) contained a total of about 74 weight % ethylene oxide based on the total weight of (b). Next, a mixture of 954 g glycerin and propylene glycol in a 62.3 to 37.7 weight % ratio (Sc) was continuously added at a combined feed rate of 8.11 g/min along with 7210 g of a mixture of propylene oxide and ethylene oxide in a weight ratio of 82/18 until a hydroxyl number of about 109 mg KOH/g was reached for the intermediate in-situ formed polyether polyol blend. The alkoxide mixture was charged at a combined feed rate of 61.28 g/min. Then, the propylene glycol and glycerin feeds were stopped and an additional 479 g of the propylene oxide and ethylene oxide mixture were continuously added until a hydroxyl number of about 106 mg KOH/g was reached for the intermediate in-situ formed polyether polyol blend. At this point the reactor contained a mixture of the previously mentioned 17.8 hydroxyl number monol (a) and 37 hydroxyl number triol (b), a diol intermediate with a hydroxyl number of 187 mg KOH/g and a triol intermediate with a hydroxyl number of 187 mg KOH/g. Next 2881 g of a mixture of propylene oxide and ethylene oxide were continuously added in a weight ratio of 55/45 at a combined feed rate of 61.28 g/min until the hydroxyl number of the diol (c) and triol (d) components reached about 140 mg KOH/g. The diol (c) and triol (d) components each contained a total of about 23 weight % ethylene oxide based on the total weight of the individual diol (c) or triol component (d). This in-situ formed polyether polyol blend contained 28.4 weight % monol (a), 14 weight % of a 37 hydroxyl number triol (b), 18.9 weight % of a 140 hydroxyl number diol (c) and 38.7 weight % of a 140 hydroxyl number triol (d). The in- situ formed polyether polyol blend had an overall functionality of about 2.4, total ethylene oxide content of about 26.3 weight % based on the total weight of the in-situ formed polyether polyol blend and an overall hydroxyl number of about 91 mg KOH/g.

Polyol G: A glycerin started poly(oxypropyleneoxyethylene) polyol having a hydroxyl number of about 37, and containing about 73% of copolymerized oxyethylene

Surfactant A: A silicone surfactant commercially available from Momentive

Performance Materials as Niax L-618

Catalyst A: An amine catalyst, commercially available from Momentive Performance Materials as Niax A-33

Catalyst B: An amine catalyst, commercially available from Momentive Performance Materials as Niax A-1

Catalyst C: Tin octoate, commercially available from Evonik as Dabco T-9

Isocyanate A: Toluene diisocyanate having 80% of the 2,4 isomer and 20% of the 2,6 isomer Isocyanate B: A low functionality polymeric diphenylmethane diisocyanate (pMDI) having an NCO content of about 32.8% and a viscosity of about 24 mPa.s at 25°C

[0103] The free-rise bench scale foams of Table 2 were prepared using the following procedure. The polyols, water, silicone surfactants, amine catalysts, and any other non-isocyanate additives were added to a cylindrical container fitted with baffles. The contents were mixed at 2400 rpm for 60 seconds with an agitator having two turbine impellers. Tin Catalyst C, if employed, was added at this time. The mixture was then degassed for 15 seconds. After degassing, the contents were mixed at 2400 rpm for 15 seconds, during which period the isocyanate was added when about 10 seconds of mixing time remained. The mixture was then poured into a 14 x 14 x 6-inch cardboard box, where it rose freely until the reaction was complete. A batch size sufficient to give a bun at least about 6 inches high was employed. The freshly prepared bun was cured for 20 minutes in an oven at 120°C and then allowed to cure at ambient conditions for a minimum of 1 day. Observations made during foaming and curing are set forth in the Tables. The buns were then trimmed to 12 x 12 x 4 inches and were roller crushed 3 times to a minimum thickness of about 0.5 inches. These samples were then conditioned for at least 16 hours at standard temperature (~23°C) and humidity (~50%) before being tested.

TABLE 1 :

Table 2: Foam Formulations In Table 2, Examples 1 , 4 and 6 are controls of an in-situ formed three component polyether polyol blend of the prior art blended with Polyol G during the process to make the foam. Examples 2, 3, 5 and 7 are representative of the invention.

Table 3A: Foam Properties Examples 1-3

Table 3B: Foam Properties Examples 4-7

Although the invention has been described in detail in the foregoing for the purpose of illustration, it is to be understood that such detail is solely for that purpose and that variations can be made therein by those skilled in the art without departing from the spirit and scope of the invention except as it may be limited by the claims.