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    • 专利摘要:
    process for the preparation of compounds derived from dopo, compound and compositions thereof. the present invention relates to a process for producing compounds derived from 9,10-dihydro-9-oxa-10-phosphaphenanthrene-10-oxide (dopo). in particular, the invention relates to the production of dopo-derived compounds by reacting dopo with diol compounds in the presence of a catalyst. the present invention also relates to the dopo-derived composition containing a high melting point diastereomer. dopo-derived compounds can be useful as flame retardants.
    公开号:BR112012024410B1
    申请号:R112012024410
    申请日:2011-03-28
    公开日:2020-01-21
    发明作者:G Mack Arthur；Yao Qiang；Junzuo Wang
    申请人:Albemarle Corp；
    IPC主号:
    专利说明:

    "PROCESS FOR THE PREPARATION OF COMPOUNDS AND DERIVATIVES OF DOPO, COMPOUND AND COMPOSITIONS OF THE SAME".
    TECHNICAL FIELD
    The present invention relates to a process for producing compounds 5 derivatives of 9,10-Dihydro-9-Oxa-10-Phosphaphenanthrene-10-oxide (DOPO). In particular, the invention relates to the production of DOPO-derived compounds by reacting DOPO with diol compounds in the presence of a catalyst. The present invention also relates to the DOPO-derived composition containing a high melting point diastereomer. DOPO-derived compounds can be useful as flame retardants.
    FUNDAMENTALS
    Phosphorus-containing flame retardants are perceived to be more environmentally friendly than halogen-containing flame retardants. In the field of epoxy resins and laminates, organo-phosphorous flame retardants with 15 reactive groups, such as those derived from 9,10-Dihydro-9-Oxa-10-Phosphaphenanthrene-10oxide (DOPO), are commonly used in resin formulations epoxy because they react with epoxy to form a phosphorus modified epoxy resin. However, "additive" otganophosphorous flame retardants, which do not have reactive groups, are not typically used in epoxy formulations, since the covalent bond between the epoxy resin and a reactive organophosphorous flame retardant is believed to be necessary to provide high glass transition temperatures and dimensional stability.
    DOPO-derived additive compounds, useful as flame retardants, were produced by reacting DOPO with halogen-containing compounds (see Japanese Kokai Patent Application No. Hei 11 [1999J-106619 and Japanese Kokai Patent Application No. P2001-270993A) . However, DOPO-derived compounds have not been produced to date by reacting DOPO with diol compounds in the presence of a catalyst.
    SUMMARY OF THE INVENTION
    The present invention relates to a process for preparing the compound
    2/28 of formula I:
    Formula I where each R 1 , R 2 , R 3 and R 4 are independently hydrogen, C 1 -C 5 alkyl, C-C 2 aryl, C 7-C 15 aralkyl or C 7-C 15 alkaryl; or R 1 and R 2 or R 3 and R 4 taken together can form a saturated or unsaturated cyclic ring, wherein the saturated or unsaturated cyclic ring can be optionally substituted by C 1 -C 6 alkyl; each m is independently 1, 2, 3 or 4; and n is 2 to approximately 18; comprising reacting a compound of formula A:
    Formula A where R 3 , R 4 in are defined above;
    with a diol compound of formula B in the presence of a catalyst, optionally a solvent, and optionally a entrainer;
    HO (CH2) rOH
    3/28
    Formula Β where n is defined above.
    The present invention also relates to a composition comprising the diastereomer of formula IIa:
    Formula lia.
    DETAILED DESCRIPTION OF THE INVENTION
    The present invention relates to a process for preparing the compound of formula I:
    where each R 1 , R 2 , R 3 and R 4 are independently hydrogen, C 1 -C 5 alkyl, C 6 -C 2 aryl, C 7- C 15 aralkyl or C 7-C 15 alkaryl; or R 1 and R 2 or R 3 and R 4 taken together can form a saturated or unsaturated cyclic ring, wherein the saturated or unsaturated cyclic ring can be optionally substituted by C 1 -C 6 alkyl; each m is independently 1, 2, 3 or 4; and n is 2 to approximately 18; comprising reacting a compound of formula A:
    4/28
    Formula A where R 3 , R 4 in are defined above;
    with a diol compound of formula B in the presence of a catalyst, optionally a solvent, and optionally a entrainer;
    HO ”(CH 2 ) n ~ OH
    Formula B where n is defined above.
    The reaction is essentially a dehydration reaction of DOPO tautomer phosphonites with diols, followed by an Arbuzov rearrangement producing the compound derived from the DOPO dimer (DiDOPO compound) and water;
    One embodiment of the present invention is where n is 2 to 6 and R 1 , R 2 , R 3 and R 4 are all hydrogen.
    Another embodiment of the present invention is a process for preparing the compound of formula II:
    5/28
    Formula II (6H-dibenz [c, e] oxafosforin, 6,6 '- (1,2-ethanediyl) bis-6,6'-dioxide) comprising reacting a DOPO compound of formula C:
    Formula C with ethylene glycol in the presence of a catalyst, optionally a solvent and optionally a entrainer.
    One embodiment in the process of making the compounds of formulas I or II is where the entrainer is present. Another modality in the process for making the compounds of formulas I or II is where both the solvent and the entrainer are present.
    The molar ratios of diol compound of formula B or ethylene glycol to DOPO compounds of formula A or IIA, respectively, can vary from approximately 0.5 to 100, or approximately 0.5 to 10, or approximately 0.6 to 5 If the ratio is too low, it leads to insufficient DOPO conversion. If the ratio is too high, it results in a large recycling of ethylene glycol.
    In one embodiment, the diol or ethylene glycol compound with the catalyst described below is slowly introduced into the DOPO, or DOPO / optional solvent / optional carrier mixture.
    The catalyst that can be used in any catalyst suitable for dehydration and Arbuzov reactions. Suitable general catalysts are alkyl halides, alkali halides, alkaline earth metal halides, transition metals and their acid halides or catalysts. Arbuzov reaction catalysts are especially suitable.
    Examples of catalysts that can be used include, but are not limited to,
    6/28 are not limited to: sodium iodide, lithium bromide, lithium chloride, potassium iodide, potassium bromide, lithium iodide, Ci-C 6 alkyl, C alkyl bromide C-6,
    2-iodoethanol, 2-bromoethanol, 2-chloroethanol, 3-iodopropanol, 3-bromopropanol, ferric bromide, ferrous chloride, ferrous bromide, manganese halide, copper powder, nickel halide, cobalt chloride, cesium bromide, chloride palladium, sulfuric acid, aryl sulfonic acid, alkyl sulfonic acid, aryl alkyl sulfonic acid, hydrochloric acid, hydrofluoric acid, oxalic acid, perchloric acid, trifluoromethane sulfonic acid, fluorsulfonic acid, nitric acid, aluminum chloride, diethyl chloride aluminum, hydrogen chloride / aluminum triethyl, ferric chloride, zinc chloride, antimony trichloride, stannous chloride, boron trifluoride, acidic zeolites, acidic clay, polymeric sulfonic acids or mixtures thereof.
    The catalyst can be added in concentrations ranging from approximately 0.01% by weight to approximately 10% by weight, or approximately 0.1 to approximately 5% or approximately 0.1% by weight to approximately 2.5% by weight, based on the total weight of the DOPO compound.
    The reaction temperature can vary from approximately 100 ° C to approximately 250 ° C, or approximately 150 ° C to 220 ° C or approximately 170 ° C to approximately 210 ° C.
    The reaction can use an optional solvent. The solvent should be chosen so that it ideally dissolves all or substantially all DOPO reagent.
    Since the reaction temperature will typically be above 100 ° C, it is preferable that a high boiling solvent is used. A high-boiling solvent is a solvent having a boiling point greater than approximately 150 ° C in 1 atmosphere and a melting point greater than approximately -100 ° C. Examples of solvents with a high boiling point include, but are not limited to: diphenyl methane, diphenyl ethane, diphenyl propane, biphenyl, decahydronaphthalene, cyclohexyl benzene, 1,3-diisopropyl benzene, dimethyl sulfoxide (DMSO), dimethyl formamide (DMF ), dimethyl acetamide (DMAC), ethylene glycol dimethyl ether, ethylene glycol diethyl ether or mixtures thereof.
    7/28
    Solvents with a lower boiling point can also be used, however, in order to get the temperature high enough the reaction would be conducted under pressure such that the reaction pressure is equal to or higher than the vapor pressure of the solvent reaction temperature. Depending on the solvent, the reaction pressure for solvents with a lower boiling point would range from greater than 1 atmosphere to approximately 10 atmospheres, or greater than 1 atmosphere to approximately 5 atmospheres, or greater than 1 atmosphere to approximately 3 atmospheres.
    Low boiling point solvents are solvents having a boiling point less than approximately 150 ° C, or approximately 100 ° C in 1 atmosphere. Examples of low boiling solvents include, but are not limited to, heptane, hexane, petroleum ether, methyl cyclohexane; toluene, xylene, mesitylene, ethyl benzene, tetrahydrofuran, 1,4-dioxane, acetonitrile or mixtures thereof.
    The amount of solvent in the reaction can vary from 0% by weight to approximately 95% by weight or approximately 30% by weight to approximately 85% by weight, or approximately 60% by weight to approximately 80% by weight based on the total weight of the reaction. reagent mixture (eg reagents, catalysts, solvents and scraper if present).
    Since the reaction generates water, it is advantageous to use a scraper to remove water to push the reaction forward. A entrainer is an organic solvent that can form azeotropes with water. The entrainer is usually a chemically inert organic liquid whose boiling points are below the reaction temperature, for example, 150 ° C and forms azeotropes with water.
    In one embodiment, the entrainer is a low-boiling solvent, where the low-boiling solvent has a lower boiling point than approximately 150 ° C in 1 atmosphere.
    Examples of scavengers that can be used include, but are not limited to, pentane, hexane, heptane, octane, cyclohexane, methyl cyclohexane, toluene, xylenes, ethyl benzene, isopropyl benzene or mixtures thereof.
    8/28
    The amount of entrainer required for total water removal can be determined in mode from the water formation calculated according to the stoichiometry of the reaction and the composition of the binary or thematic azeotrope. It has been found useful to use the excess entrainer, advantageously in an amount that is 50 to 200% by weight above the amount theoretically calculated.
    The entrainer may or may not be the same as the solvent. If the carrier is different from the solvent, the amount of carrier can vary from approximately 0% by weight to approximately 30% by weight or approximately 1% by weight to approximately 30% by weight, or approximately 2% by weight to approximately 15% by weight. weight based on the total weight of the reagent mixture (eg reagents, catalysts, solvents or scraper if present).
    In a particularly useful embodiment of the process of the invention, the entrainer is added to the reaction mixture before the ethylene glycol or diol compounds. After a mild reflux is observed, the addition of diol or ethylene glycol with catalyst is initiated. The progress of the reaction can be followed in a simple way by collecting and separating the distilled diol / water / entrainer mixture. The entrainer and diol separated from the azeotrope can be resumed directly, that is, without a purification step intermediate to the reaction.
    In one embodiment, the process is conducted at normal pressure and the entrainer is continuously recycled back to the reactor.
    The entrainer can also be replaced by vacuum and / or inert gases, such as nitrogen, carbon dioxide and / or helium as long as the water generated in the process can be removed effectively.
    The reaction can be carried out in batch or continuous mode. A series of reaction vessels with mixers can be used for continuous mode. When in continuous mode, an excess of diol or ethylene glycol compound is used and can be recycled back into the process for further reaction.
    The reaction time may vary depending on the reaction temperature, type and quantity of catalyst, and the use, type and quantity of a solvent and / or entrainer. Typically, the reaction time will be approximately 0.5 to
    9/28 approximately 48 hours or approximately 1 to approximately 24 hours.
    After the reaction, the product resulting from formulas I or II can be purified using any conventional method, such as distillation, washing, filtration and / or drying. In one embodiment, water or water-miscible solvents such as alcohols (eg isopropanol), aldehydes or ketones (eg acetone) are used to wash the product before and / or after filtration.
    The peak melting point of the compound of formula II is preferably greater than approximately 245 ° C or approximately 250 ° C. To determine the peak melting point, a differential scanning calorimeter (DSC) can be used, such as a “TA Instruments Q200” analyzer with its standard DSC cell. The DSC is connected to a PC, which provides user interface and operating system control. The temperature scale is calibrated at 10 ° C / min. using the melting points of reference standards for gallium, indium, lead and zinc. The flow heat scale is calibrated using the indium fusion heat. The baseline response is calibrated at 20 ° C / min. with a standard of synthetic sapphire heat capacity. All of these calibrations must be performed in accordance with the instrument manufacturer's recommended procedures.
    The samples are passed through a gold-plated stainless steel crucible at 10 ° C / min. from 0 ° C to 400 ° C. A raw data file containing the sample heat flow and temperature data is saved to the PC's hard drive during measurement. After the DSC measurement is finished, the raw data file is analyzed for melting behavior. The melting endotherm is integrated for yield, extrapolated start temperature, peak temperature and heat of fusion.
    TA Instrument software is used to determine the peak melting point by selecting temperature points above and below the peak. If a sample has multiple peaks, then multiple peak melting points will be reported. The peak melting point is the maximum endotherm for a specific melting transition. The maximum peak determination is an analysis used to determine the most remote point, in relation to the baseline, within the chosen limits.
    Composition of Diastereomer with High Melting Point
    10/28
    This invention also relates to a composition comprising the diasteromer of formula 11a:
    Formula ΠΑ.
    It has been found that using the process of the present invention, a mixture of stereoisomers is produced. For the compound of formula II, at least three stereoisomers are produced in the composition. One is the high melting diastereomer of formula IIa and two are lower melting enantiomers of formula IIb and IIc.

    Formula Ilb
    It is sometimes beneficial to choose a composition with a higher amount of constituents with a high melting point. A composition with a higher “Isomer Ratio” of constituents of high melting point vs. low melting point constituents would be more desirable for high temperature polymer applications.
    In the present application, the Isomer Ratio can be calculated from curves
    DSC as follows:
    11/28
    Isomer Ratio - Ah / (Ah + A t ), where Ah: high melting point peak area and Ai: low melting point peak area.
    Another method of calculating the Isomer Ratio is 31 P NMR as follows:
    Corrected ratio = (A h -Ai x 0.5) / (A h + Ai), where A h : high peak field area and Ap low peak field area.
    The uncorrected ratio = A h / (A h + AQ, where A h and Ai are defined above.
    It was found that a corrected ratio obtained from 31 P NMR is close to values obtained from the DSC curves and, therefore, a corrected ratio is always assumed if there is no explicit statement on the Isomer Ratios obtained from 31 P NMR.
    Method 31 P NMR
    A NMR spectroscopy procedure that can be used to measure the Isomer Ratio is discussed below. This procedure is appropriate for the determination of the Isomer Ratio by normalizing weight percent.
    Core: 31P; Proton decoupled; Pulse program: zgig30; Data points collected (TD): 205k; Spectral Width (SWH): -40322 Hz; Prepulse delay (Dl): 20 s minimum (use appropriate pre-pulse delay to ensure that all observed cores have adequate relaxation time); Acquisition (NS): 16 scans minimum (scans sufficient to provide good signal for noise); Blocking solvent: CDC13. Referenced to 85% aqueous phosphoric acid.
    The chemical displacement of the isomer with a high melting point appears in the region of high magnetic field around 36.9 ppm and the chemical displacement of the low-ion point isomers appears in the region of low field around 37.1 ppm.
    In one embodiment, the composition comprises a plurality of the diastereomer of formula 11a. In other embodiments, the composition has an Isomer Ratio greater than approximately 0.5, or greater than approximately 0.6, or greater than approximately 0.7, or greater than approximately 0.8, or greater than approximately 0.9, or greater than approximately 0.95 or greater
    12/28 than approximately 0.98, based on the use of DSC or Method 31 P NMR. For Method 31 P NMR, the Isomer Ratio is the corrected Isomer Ratio.
    Process for Obtaining Higher Melting Point Isomers:
    In another embodiment, the present invention relates to a method for producing a higher melting point composition comprising the compound of formula II:
    Formula II comprising contacting a composition which contains lower amounts of high melting point isomers of formula II with alcohols, water, or mixtures thereof in the presence of an acid catalyst, thereby producing a composition containing larger amounts of point isomers highest melting point of formula II.
    Low melting point isomers can be converted to high melting point isomers in the presence of alcohols and / or water at a temperature ranging from 0 to 300 ° C. This isomerization is catalyzed by acid catalysts that include mineral acids and Lewis acids. Mineral acids include sulfuric acid, methanesulfonic acid, hydrochloric acid, phosphoric acid, phosphonic acids and phosphoric acids. Lewis acids are defined as a molecular entity that is an electron pair acceptor and include aluminum chloride, zinc chloride, ferric chloride, etc.
    Examples of such acid catalysts include, but are not limited to: sulfuric acid, aryl sulfonic acid, alkyl sulfonic acid, aralkyl sulfonic acid, hydrochloric acid, hydrobromic acid, hydrofluoric acid, oxalic acid, perchloric acid, trifluoromethane sulfonic acid, fluorsulfonic acid, nitric acid, phosphoric acid, phosphonic acids, phosphonic acids, aluminum chloride, diethyl aluminum chloride, hydrogen chloride / aluminum triethyl, ferric chloride, zinc chloride, trichloride
    13/28 antimony, stannous chloride, boron trifluoride, acidic zeolites, acidic clays, polymeric sulfonic acids or mixtures thereof.
    One way to perform isomerization is to feed a mixture of alkylene glycol (eg ethylene glycol) and water to the DOPO solution at a temperature of 25 to 300 ° C at elevated pressure or normal pressure. As the DOPO + alkylene glycol reaction produces water on the spot, the mixture of alkylene glycol and water can be replaced with pure alkylene glycol on the condition that the water generated is not completely removed in a precise manner so that it can participate in the isomerization . Otherwise, a mixture of alkylene glycol and water is required. This mixture can be recovered alkylene glycol and water, which are co-distilled and condensed during the reaction, or can be obtained by mixing alkylene glycol with water.
    The mixture of alkylene glycol and water can be added at the beginning of the reaction where the DOPO conversion is essentially zero, during the reaction, and / or after the reaction where DOPO is essentially consumed. If the mixture of alkylene glycol and water is added after DOPO is consumed, the mixture can be replaced with water alone, alcohols or their combinations as they do not interfere with the reaction anymore except isomerization.
    A preferred embodiment of the above process is when the alkylene glycol is ethylene glycol.
    The required acid catalysts are preferably those generated at the site during the reaction; however, external acids can be added to accelerate both the reaction and isomerization.
    A second embodiment includes the treatment of finished compounds of formula I or II containing a small amount (for example, <15%) of isomers with a high melting point for alcohols and / or water in the presence of acid catalysts and in the presence or absence of solvents high pressure or normal pressure in a temperature range of 25 to 300 ° C. The treatment is carried out by mixing alcohols, and / or water, acid catalysts, and DiDOPO containing a small amount (for example, <15% by weight) of high melting isomer (s). This mixture is then heated to a
    14/28 temperature range from 25 to 300 ° C for a period of time until the desired isomer ratio is obtained. Usually the time period ranges from a few minutes to 10 hours, preferably from 0.5 to 8 hours, more preferably from 1 to 5 hours. The amount of catalyst is 0.1% to 50% DiDOPO, preferably 1 to 25%, more preferably 5 to 15%. The temperature is 25 to 300 ° C, preferably 50 to 250 ° C, more preferably 80 to 200 ° C. This method is particularly advantageous for converting the finished DiDOPO which is largely composed of low melting isomers to high melting DiDOPO.
    Use of Compounds of the Invention
    The present invention also relates to a flame retardant polymer composition comprising a polymer and the flame retardant amount of the compounds of the formula I, II, IIa, IIb, IIc or mixtures thereof.
    The polymer that can be used in the flame retardant polymer composition includes, but is not limited to: polyolefins, polyesters, polyethers, polyketones, polyamides, polyvinyl chlorides, natural and synthetic rubbers, polyurethanes, polystyrenes, poly (meth) acrylates, phenolic resins, polybenzoxazine, polyacetals, polyacrylonitriles, polybutadienes, polystyrenes, polyimides, polyamideimides, polyetherimides, polyphenyl sulfides, polyphenylene oxide, polycarbonates, cellulose, cellulose derivatives, cyanate esters, polyphenylene resins, polyphenylene resins, polyphenylene resins styrene, butadiene-divinylbenzene-styrene resins, epoxy-modified polybutadiene resins, vinyl or acrylic acetate adhesives, carboxyl-terminated butadiene-acrylonitrile copolymers, phenylene ethers, butadiene-styrene copolymers grafted with maleic anhydride 4-methyl-l pentene modified by maleic anhydride, copolymer those of maleatated 1-butene-ethylene, resins derived from benzyl vinyl ether compounds, epoxy resins or mixtures thereof. Preferably, the polymers are polyolefins, polyesters, phenolic resins, phenol triazine novolacs, cresol triazine novolacs, phenol triazine epoxy novolacs, cresol triazine epoxy novolacs, polyamides, polyurethanes, polystyrene, epoxy resins or mixtures of the same.
    15/28
    Another modality is when the flame retardant composition also comprises at least one conventional additive, such as heat stabilizers, light stabilizers, ultraviolet light absorbers, antioxidants, antistatic agents, preservatives, adhesion promoters, fillers, pigments, dyes, lubricants, mold release agents, blowing agents, fungicides, plasticizers, processing aids, acid eliminators, dyes, pigments, nucleating agents, wetting agents, dispersing agents, synergists, mineral fillers, reinforcing agents, such as fiberglass , glass flake, carbon fiber, or metal fiber; wires such as potassium titanate, aluminum borate or calcium silicate; inorganic fillers and other flame retardant additives; smoke suppressors and mixtures thereof.
    Other flame retardant additives that can be used with the compounds of formulas I, II, IIa, IIb, IIc or mixtures thereof include, but are not limited to, nitrogen-containing synergists, such as ammonium polyphosphate, melamine, phosphate melamine, melamine cyanurate, melamine pyrophosphate, melamine polyphosphate, guanidine and piperazine cyanurate and phosphate derivatives, phosphazene compound, polyphosphazenes, antimony oxide, silica, talc, hydrotalcite, borate salts, hydrated alumina, such as hydrated alumina aluminum (ATH), bohemite, bismuth oxide, molybdenum oxide or mixtures of these compounds with zinc, aluminum and / or magnesium oxide or salts.
    The amount of compounds of the formula I, II, IIa, IIb, IIc or mixtures thereof added to the polymer as a flame retardant can vary over a wide range. Usually from approximately 0.1 to approximately 100 parts by weight of the compounds are used per 100 parts by weight of polymer. Preferably approximately 0.5 to approximately 70 parts of the compounds are used per 100 parts by weight of polymer, or from approximately 2 to approximately 50 parts by weight per 100 parts by weight of polymer.
    Preferably, the compounds of the formula I, II, IIa, IIb, IIc or mixtures thereof are ground or ground before combining with the polymer the particle size of the ground after grinding or grinding may be less than approximately 15
    16/28 pm, or less than 10 pm, or less than approximately 5 pm, or less than approximately 3 pm or less than approximately 2 pm. The particle size d 50 can be even less than 1 pm, such as approximately 100 nm to 800 nm. A dso particle size is the median particle size, where half of the particles are above the value and half of the particles are below the value. Any suitable grinding or grinding technique can be used as a jet grinder.
    To determine median particle size, an LS-230 Coulter counter or equivalent is used with its small volume module. The manufacturer's operating instructions are followed. Alternatively, a Horiba laser light scattering instrument (for example, Horiba LA900 Model 7991) or equivalent can be used. The procedure involves weighing the sample, typically an amount in the range of approximately 0.01 gram to approximately 0.015 gram, in a clean dry aluminum cup that was washed with deionized water before use. The self-sampling instrument disperses a 0.05 g sample in water using 0.4 ml of 1% Triton X-100 surfactant and ultrasonic treatment. This suspension is circulated through a measuring cell where the dust particles scatter a beam of laser light. Detectors in the instrument measure the intensity of the scattered light. The computer in the instrument calculates average particle size, average particle size and particle size distribution for such measurements.
    Polymer master batches containing the compounds of the formula I, IIa, IIb, IIc or mixtures thereof of the present invention, which is mixed with additional amounts of substrate polymer, may contain even higher concentrations of the compounds, for example, approximately 10 to approximately 1000, or from approximately 25 to approximately 500, or from approximately 25 to approximately 250 parts by weight of the compounds per 100 parts by weight of the polymer.
    Alternatively, the amount of the phosphorus compounds of the formula I, II, IIa, IIb, IIc or mixtures thereof in the flame retardant polymer composition is selected so that the composition will contain approximately 0.1% in
    17/28 weight at approximately 10% by weight, or approximately 1.0% by weight at approximately 7% by weight or approximately 1.2% by weight at approximately 5% by weight or approximately 1.5% by weight at approximately 4 % by weight of phosphorous content, based on the total weight of the composition.
    EXAMPLES
    The following examples illustrate the present invention. It should be understood, however, that the invention as fully described here and as mentioned in the claims, is not intended to be limited by the details of the following examples.
    EXAMPLE 1
    6H-Dibenzrc.e] ri.21oxafosforin, 6.6 ’- (1,2-ethanediyl) bis-.6.6’-dioxide
    To a reaction flask with 3 25 ml necks fitted with a Dean-Stark collector, addition funnel, thermocouple and nitrogen inlet and outlet, 17.082 g DOPO (0.0790 mol), 2.550 g of ethylene glycol (0, 0404 mol) and 0.300 g of sodium iodide (0.00200 mol). The reaction mixture was heated to 210 ° C and the addition of p-xylene (entrainer) from the addition funnel was started. The water immediately came out with p-xylene and ethylene glycol. After the reaction temperature was maintained between 190210 ° C for 2 hours, another amount of 1.651 grams of ethylene glycol was added to compensate for that loss. The reaction mixture was kept under stirring for another hour and then the mixture was diluted with xylene and stirred for half an hour at 133 ° C. The paste was filtered, washed with acetone and dried at 120 ° C overnight. A white solid of 14.84 grams was obtained and the yield was 82%.
    EXAMPLE 2
    6H-Dibenzrc, eiri.21oxafosforin, 6.6 ’- (1.2-ethanediyl) bis-.6,6’-dioxide
    To a reaction flask with 3 250 ml necks fitted with a Dean-Stark collector, two addition funnels, thermocouple and nitrogen inlet and outlet were charged 80.64 g (0.373 mol) DOPO. The flask was heated and the temperature was brought up to 170 ° C. the addition of p-xylene from an addition funnel was started. After a gentle xylene reflux in a Dean-Stark collector was observed, a mixture of 16.682 g (0.269 mol) of ethylene glycol in 1,019 g of methyl sulfonic acid was gradually added from the second addition funnel. The reaction mixture was kept under stirring
    18/28 in a temperature range of 170 to 180 ° C for 18 hours, then the reaction temperature was lowered to 100 ° C. the obtained paste was washed with a mixture of 140 g of water and 11.06 g of 50% sodium hydroxide, then filtered, washed with water and dried in an oven. A white solid of 42.125 g corresponding to a 50% yield was obtained. The uncorrected 31PNMR isomer ratio of high melting point / low melting isomer = 0.87. The corrected ratio was 0.80.
    This example demonstrates that by keeping the reaction temperature low so that the removal of water was not timely a product with a very high content of high melting point isomer was obtained.
    EXAMPLE 3
    6H-Dibenzrc, eiri .21oxafosforin, 6.6 ’- (1.2-ethanediyl) bis-, 6,6’-dioxide
    To a 500 ml 4-neck reaction flask equipped with a Dean-Stark collector, a mechanical stirrer, two addition funnels, thermocouple and nitrogen inlet and outlet were charged 87.30 g (0.404 mol) of DOPO, 27, 4 g of p-xylene, and 178 g of diphenyl propane. The mixture was brought to a temperature of 200 ° C and more p-xylene was added to ensure smooth reflux in a Dean-Stark collector. The addition of a mixture of 43.037 g (0.693 mol) of ethylene glycol and 0.884 g of sodium iodide was then started and completed in 5.5 hours. A mixture of aqueous distillate was recycled back to the addition funnel and the addition was completed in 6 hours. A paste was observed with good agitation. A sample was taken and 31P NMR indicated that the paste was composed of 93% DiDOPO and 7% another species containing phosphorus. The paste was mixed with 19 g of isopropanol and stirred for half an hour at a temperature of 86 ° C, then it was filtered, washed with 2 x 40 g of isopropanol, and dried in an oven at a temperature of 130 ° C during night. A white solid of 81.2 g was obtained with a purity> 99%. The isolated yield was 88%. The uncorrected isomer ratio of high melting point / low melting isomer = 0.69. The corrected ratio was 0.53.
    This example demonstrates that by feeding a mixture of ethylene glycol and water during the reaction a product rich in the high melting point isomer (s) was obtained.
    19/28
    EXAMPLE 4
    6H-dibcnz | c, eiri .21oxafosforin, 6.6 ’- / 1.2-ethanediyl) bis-, 6,6’-dioxide
    To a reaction flask with 3 250 ml necks equipped with a Dean-Stark collector, a magnetic one, two addition funnels, thermocouple and nitrogen inlet and outlet were loaded 46.778 g (0.216 mol) DOPO, 16.50 g of p -xylene, and 106.70 g of diphenyl methane. The mixture was brought to a temperature of 200 ° C and more p-xylene was added to ensure smooth reflux in the Dean-Stark collector. The addition of a mixture of 25.407 g (0.393 mol) of ethylene glycol and 0.639 g of sodium iodide was then started and completed in 6 hours. A mixture of aqueous distillate was recycled back to the addition funnel and the addition was completed in 2 hours. A paste was observed with good agitation. A sample was taken and 31 P NMR indicated that the paste was composed of 93% DiDOPO and 7% other species containing phosphorus.
    EXAMPLE 5
    6H-Dibenz1 [1,21oxafosforin, 6.6 ’- (1,2-ethanediyl) bis-, 6,6’-dioxide
    Following Example 4, except that biphenyl was used as a solvent. The paste of the final mixture was composed of 91% of DiDOPO and 9% of another species containing phosphorus.
    EXAMPLE 6
    6H-Dibenz | c.el Γ1,21oxafosforin, 6,6 ’- (1,3-propanediyl) bis-6,6,’ - dioxide
    To a 100 ml 3-neck reaction flask equipped with a Dean-Stark collector, a magnetic collector, two addition funnels, thermocouple and nitrogen inlet and outlet were loaded with 33.004 g (0.153 mol) of DOPO and 5.361 g of p- xylene. The mixture was brought to a temperature of 200 ° C following the addition of a mixture of 7.405 g (0.0973 mol) 1,3-propanediol and 0.631 g of sodium iodide was started and completed in 1.6 hours. A mixture of aqueous distillate was recycled back to the addition funnel and the addition was completed in 1 hour. Repeat this procedure twice and a sample was taken. 31 P NMR indicated that the solution was composed of 55% DiDOPO, 30% mono-species and 15% other species containing phosphorus.
    EXAMPLE 7
    20/28
    High Pressure Process
    ÓH-Dibenzlc.el Γ1,21oxafosforin.6,6 ’- (1,2-ethanediyl) bis-, 6,6’-dioxide
    To a 100 mL autoclave equipped with a mechanical stirrer, thermocouple, distillation column and collection vessel, 10.80 g of DOPO, 3.1 g of ethylene glycol, 50 g of p-xylene (solvent / entrainer) and 0.188 g of sodium iodide. The reaction mixture was first swept by nitrogen flow for 15 minutes and then gradually brought to a temperature range of 190 to 200 ° C at 0.276 to 0.283 MPa (40 to 41 psig). Liquid started to come out at 194 ° C. After no more liquid left, the reaction temperature was slowly raised to 200 ° C and the mixture was easily stirred for 2 hours. After cooling and degassing, the NMR analysis showed that the crude paste contained 62% DiDOPO, 22% DOPO and the rest being phosphorus-containing species. Another amount of 0.78 g of ethylene glycol and 28 g of p-xylene was added to the reactor and heated to 190 to 200 ° C. After 5 hours, the reaction mixture was cooled and diluted with 22 g of p-xylene and 10 g of iso-propanol. NMR analysis indicated 90% DiDOPO.
    EXAMPLE 8
    6H-Dibenz [c, eiri, 21oxafosforin.6,6 ’- (1,2-ethanediyl) bis-, 6,6’-dioxide with a relatively low Isomer Ratio
    To a reaction flask with 4 necks of 500 ml equipped with a Dean-Stark collector, a mechanical stirrer, two addition funnels, thermocouple and nitrogen inlet and outlet were loaded 88.36 g (0.409 mol) DOPO, 43.60 g of p-xylene and 177 g of diphenyl methane. The mixture was brought to a temperature of 200 ° C to obtain a gentle reflux in a Dean-Stark collector. The addition of a mixture of 61.84 g (0.996 mol) of ethylene glycol and 0.925 g of sodium iodide was then started and completed in 14.5 hours. A sample was taken and 31 P NMR indicated that the paste was composed of 82% DiDOPO, 9% phosphonic acid and another species containing phosphorus. The uncorrected ratio of high melting point isomer (s) to total isomers = 0.41. The corrected ratio is 0.12. This example demonstrates that by feeding water-free ethylene glycol a product rich in low melting point isomers was obtained. A summary of some of the examples is shown below in Table 1.
    21/28
    TABLE 1. SUMMARY OF EXAMPLES
    Example 1 2 3 4 5 7 8 Way of DOPO / EG / cat. EG / cat. EG / cat. EG / cat. DOPO / EG / EG / cat. charge EG Added Added Added Added catalyst Addedcatalyst continuously to be continued- to be continued- to be continued- loaded one continuouslyloadedmind and mind and mind and instead, system withoutoncerecycled recycled recycled closed recycling Catalyst NaI Methyl acid NaI NaI NaI NaI NaI _sulfonicTemp (° C) 190-210 170-175 190-200 190-200 190-200 190-200 190-200 Dragger p-xylene p- xylene p- xylene p- xylene p- xylene xylene xylene Solvent No No Diphenyl Diphenyl methane Biphenyl Xylene Diphenyl methane propane Gross income 93% 91% 92% 90% 82% Yield 82% 50% 88% 83% ' ·· isolated Capacity Difficult A bit of Easy Very easy Very easy Good Easy agitationdifficultyReason for 31 pnmr 0.51 0.87 0.69 0.62 0.58 0.57 0.41 Ratio for 31 P NMR- corrected 0.26 0.80 0.53 0.43 0.37 0.36 0.12 Reason for0.82 0.61 DSC----
    Corrected ratio - (low field peak area - 0.5 * high field peak area) / (low field peak area + high field peak area).
    EXAMPLE 9
    22/28
    6H-Dibenz [c, e] [1.21oxaphosphorin.6,6 > - (1,2-ethanediyl) bis-.6.6 , -dioxide
    To a reaction flask with 3 necks of 500 ml adapted with a Dean-Stark collector, an addition funnel, thermocouple and nitrogen inlet and outlet, 89.0 g (0.412 mol) DOPO, 40.9 g of p- xylene, 182.8 g of diphenyl methane. The mixture was heated and the temperature was brought up to 200 ° C. After a gentle reflux of xylene in the Dean-Stark collector was observed, a mixture of 61.895 g of ethylene glycol with 0.918 g of sodium iodide was gradually added from the addition funnel. The reaction mixture was maintained by stirring in a temperature range of 190 to 200 ° C. After approximately 16 hours, the EG / Nal mixture was used and 48 mL of 10 EG / H20 recovered from the distillate were fed continuously over a temperature range of 200 to 25 ° C and completed in 4 hours. Then the mixture was then heated back to 190 ° C to remove ethylene glycol and water in ~ 1 hour. After cooling, the reaction mixture was subjected to isopropanol filtration and washes and then dried at 130 ° C. Samples were taken during the reaction and the isomer ratios were measured by 31 P NMR. Since the reaction generated by-products, the isomer ratios were normalized. The results are shown in Table 2.
    TABLE 2. MELTING POINT ISOMER CONTENT (MP)
    HIGH VS. REACTION TIME IN EXAMPLE 9
    Time(H) EG / Remaining final (ml) eg / h 2 o added (ml) Phosphonic acid (mol%) DOPO conversion (%) Isomer ofHigh mp Isomer ofHigh MP (% corrected) (% corrected) no 13.5 69 93 44 17 14.6 211 98 49 24 16.1 0 0 11 100 52 28 17.1_ 1152 28 18.112 1161 41 20.625 1160 40 21.648 1188 J2
    23/28
    This example demonstrates that high melting isomer (s) can be obtained by converting low melting isomer to ethylene glycol and water in the presence of acid catalysts.
    EXAMPLE 10
    6H-Dibenz [c, e] [1,2] oxaphosphorin. 6.6 ’- (1,2-ethanediyl) bis-, 6,6’-dioxide
    A 6H-Dibenz [c, e] [1,2] oxafosforin composition, 6,6 '- (1,2ethanediyl) bis-, 6,6'-dioxide (7,866 g) containing 88% low point isomer The melt was mixed with 85% aqueous phosphoric acid (0.189 g) and diphenyl propane (42 g). The mixture was gradually heated to 200 ° C and maintained at this temperature for 2.5 hours. Samples were taken during treatment and measured by 31P NMR. The results were shown in Table 3 below:
    TABLE 3. ISOMER CONTENT VS. REACTION TIME FOR EXAMPLE 10
    Time (h.) Low% Mp Isomers High Mp Isomer% 0 88 12 1 81 19 2.5 48 52
    This example demonstrates that the treatment of 6Hdibenz [c, e] [1,2] oxafosforin, 6,6 '- (1,2-ethanediyl) bis-, 6,6'-isomer rich with low melting point by aqueous acid catalyst at elevated temperature increased the isomer content with a high melting point.
    EXAMPLE 11 ^ H-Dibenz [c, e] [1,2,2oxaphosphorin, 6.6 ’- (1,3-propanediir) bis -., 6,6’-dioxide
    The composition of 6H-Dibenz [c, e] [1,2] oxafosforin, 6,6 '- (1,2-ethanediyl) bis, 6,6-dioxide (57.9 g, isomer ratio = 0.43 , low fusion isomer = 0.57) was mixed with 134.5 g of diphenyl methane and 3.1 g of 85% phosphoric acid in a flask equipped with additional funnel, Dean-Stark collector, mechanical stirrer and thermocouple. The mixture was heated to 150 ° C. Water (13 g) was slowly added to the reaction mixture and continuously distilled. After 12 ml of water was collected, the reaction was adjusted to full reflux and the reaction mixture was stirred for 2.5 hours at that time.
    24/28 temperature. Then, the reaction temperature was lowered to 126 ° C and isopropanol (70.4 g) was added. The mixture was subsequently cooled, filtered, washed with 82 g of isopropanol and dried at 130 ° C in an oven overnight. A sample was taken and the result of 31 P NMR showed an isomer ratio of 0.90 (low fusion isomer = 0.10).
    This example demonstrates that treating 6H-dibenz [c, e] [1,2,2] oxaphosphorin, 6,6 '(1,2-ethanodnl) bis-, 6,6'-isomer rich with low water melting point in the presence of an acid catalyst, the isomer content increased with a high melting point.
    EXAMPLE 12
    6H-Dibenz [c, e] [1,2] oxafosforin, 6.6 ’- (1,3-propanediyl) bis-, 6.6’-dioxide
    To a 1 L reaction flask equipped with a mechanical stirrer, thermometer, pressure gauge and Dean-Stark collector were charged 100.00 g DOPO, 0.10 g sodium lodide, 0.28 g ethylene glycol and 400 g of mixed xylenes. The reaction mixture was heated to 200 ° C at approximately 0.276 MPa (40 psig). A solution of 0.90 g of sodium iodide in 50.00 g of ethylene glycol was gradually fed into the mixture over a course of 14 hours. Subsequently the mixture was kept under stirring at 198 at 200 ° C for 6 hours. A paste sample was then taken. 13 P NMR showed that DOPO was essentially consumed with a product isomer ratio = 0.43 and the presence of phosphonic acid (approximately 3 mole% DOPO). To increase the isomer ratio, water (120 g) was slowly fed to the reaction mixture at 173 ° C over a 5 hour course. At the end of the water treatment, a sample was taken and 31 P NMR showed a product isomer ratio = 0.94.
    This example demonstrates that a high melting point isomer (s) can be obtained by converting a low melting point isomer into water.
    EXAMPLE 13
    Use of 6H-Dibenz | c, e] [L2] oxafosforin, 6.6 ’- (T.2-butanediir) bis-.6.6’dioxide as a flame retardant in epoxy laminate
    25/28
    DOPO
    195-200 ° C
    -xylenes
    Cat. Nal
    Ethylene glycol (EG)
    Di-DOPO
    High-purity DOPO was loaded into a reactor and a given amount of mixed xylenes was then pumped into the reactor. A 2.62% by weight NaI / EG solution was prepared and loaded into the reactor. The contents were then stirred and heated to 198 ° C in 5 to 6 hours while the pressure was maintained at 0.276 to 0.283 MPa (40 to 41 psig). After the content reached the reaction temperature, a co-fermentation containing 2.62% by weight NaI / EG and mixed xylenes was initiated. Coalimentation lasted a minimum of approximately 14 hours.
    The xylene feed rate was around 0.45 kg / min (1 Ib / min). After feeding for 11.5 hours and holding for 2 hours, the reactor became full. It was cooled to 190 ° C, and a sample of the reactor paste was collected. The NMR results indicated that the DOPO conversion was approximately 72% at that point. The reactor was heated again to 197-199 ° C, and co-feeding was carried out for another period of 5 hours, followed by retention of 2.5 hours. The DOPO conversion was then approximately 93% at the end of the second co-feed. The reaction mixture was quenched with IPA and cooled slowly to ~ 100 ° C.
    After cooling, the reactor contents were filtered and the wet mass was then washed three times with new IPA and dried under vacuum at 130 ° C.
    Approximately 100 g of the sample prepared above was added to a 2L Erlenmeyer flask, along with 2.0 kg of chloroform and 0.4 kg of 2propanol. The mixture was stirred for approximately 15 minutes at 65 ° C. The mixture was removed from heat and allowed to cool slowly without stirring to room temperature. The conical flask was then placed in an ice bath for approximately 1 hour. The white solid was vacuum filtered through a medium glass frit funnel, rinsed with approximately 100 ml of 2-propanol and dried at 170 ° C for 5 h. Three
    26/28 batches of the resulting dry powder were combined and jet milled into a smaller particle size having a d50 of approximately 2 to 4 pm to provide 130 g of a sample of 6H-dibenz flame retardant [c, e] [l , 2] oxafosforin, 6,6 '- (1,2-butanodnl) bis-, 6,6'-dioxide with very high purity. The sample isomer ratio was approximately 0.98.
    In general, stock solutions of advanced resin, dressing and promoter are all prepared and stored separately to facilitate experimentation. A 50 wt% novolac epoxy o-cresolfenol resin solution, NPCN®-703 (Nan Ya Plastics Corporation), containing 50 wt% 2-butanone (MEK) was prepared. Novolac Durite SD-1702 curing agent was obtained from Hexion Corporation. A novolac resin solution was prepared by dissolving 50% by weight of SD-1702 in 50% by weight of MEK solvent.
    A mixture of flame retardant resin containing 3.0% by weight of P was prepared by mixing 128.8 g of 50% by weight NPCN 703 solution, 62.7 g of 50% by weight SD-1702 solution. , 14.0 g of flame retardant, 14.0 g of melamine polyphosphate Melapur 200 (M-200) from BASF Corporation and 0.070 g of 2-phenyl imidazole promoter. An additional 11 g of MEK was added to the mixture. The ratio of novolac to promoter was approximately 448. The flame retardant was insoluble in the resin solution until it made contact with the hot gel plate, where it dissolved completely at elevated temperature. Approximately 0.5 to 1 ml of the resin mixture was added to a hot curing plate (Thermoelectric company) at approximately 170 to 172 ° C. A tongue depressor was split in half lengthwise and half of the depressor was used to move the ream on the hot plate until stiffness was observed and then raising the resin with the flat part of the depressor until the rope formation ceased . The gel time was 3 minutes, 16 seconds, determined by the point where "strings" of resin could no longer be pulled from the resin mixture and the epoxy became "free of grip". The resin mixture was mixed thoroughly using a high shear mixer stirred at 6,000 RPM for approximately 15 minutes.
    A 27.94 by 27.94 cm (11 inch) woven glass fabric
    27/28 by 11 inches) (7628 glass and 643 finish from BGF Industries) was cut to the size of a large roll and stapled onto wooden supports (30.48 cm (12 inches) long, 2.54 cm (1 inch) ) wide and 0.16 cm (1/16 inch) thick) at the top and bottom ends of the fabric. The wooden supports contained holes in the corners to insert paper clips on one end to hang the fabric in the stage B oven. Stage A, or resin varnish, was painted on the front and back of the fabric. Paper clips were unfolded and inserted into the holes in a wooden support. The saturated resin fabric was suspended from aluminum supports in a laboratory hood and allowed to drip until dry for approximately one minute before hanging in a Blue M oven with preheated forced air (up to 170 ° C) (Lab Safety Supply Inc ., a General Signal unit) for 1 minute. 20 seconds. The edges of the pre-impregnated stage B composite have been removed by reducing the sheet dimensions to 25.4 by 25.4 cm (10 inches by 10 inches). The sheet was cut into four 12.7 by 12.7 cm (5 inch by 5 inch) sheets and weighed before stacking the four layers of pre-impregnated composite between two layers of Pacothane release film (Insulectro Corp.) and two steel plates (square dimensions 0.32 cm (1/8 inch) thick, 30.48 by 30.48 cm (12 inches by 12 inches)). The laminate was formed in the hot press at 34,474 MPa (5,000 psig) for 1 hour. The resulting laminate was 0.08 cm (0.03 inch) thick, contained 45.5% by weight of resin and was subjected to overflow of resin at 17% by weight during pressing. Five coupons with 1.27 cm (0.5 inch) width were cut from the laminate using a diamond saw and the edges of the coupon were smoothed with sandpaper. The flammability of the coupons was rated by ASTM D3 801-06 using an Atlas UL-94 firing chamber, resulting in a V-O rating with 29 seconds of total burning time for the two ignitions in all five coupons. No single burn was longer than 10 seconds.
    The glass transition temperature of the laminate was approximately 185 ° C and the TGA was approximately 322 ° C for a loss of 1%, approximately 342 ° C for a loss of 2% and approximately 363 ° C for a loss
    28/28 loss of 5%.
    The components mentioned by the chemical name or formula elsewhere in the specification or claims of the present, whether mentioned in the singular or plural, are identified since they exist before coming into contact with another substance mentioned by the chemical name or chemical type (for example, other component, solvent, or etc.). No matter what chemical changes, transformations and / or reactions, if any, occur in the resulting mixture or solution as such changes, transformations and / or reactions are the natural result of assembling the specified components under the conditions required in accordance with that disclosure. In this way the components are identified as ingredients to be brought together in relation to the execution of a desired operation or in the formation of a desired composition. In addition, although the following claims may refer to substances, components and / or ingredients in the present ("comprises", "is", etc.) the reference is in relation to the substance, component or ingredient as it existed at the time just before to be first contacted, mixed or stirred with one or more other substances, components, and / or ingredients in accordance with the present disclosure. The fact that a substance, component or ingredient may have lost its original identity through a chemical reaction or transformation during the course of contact, mixing or stirring operations, if conducted in accordance with that disclosure and with the common knowledge of a chemist, it has no practical importance.
    The invention described and claimed here should not be limited in scope by the specific examples and the modalities disclosed herein, since those examples and those modalities are intended to be illustrations of various aspects of the invention. Any equivalent modalities are intended to be within the scope of the invention. Indeed, various modifications of the invention in addition to those shown and described here will become apparent to those skilled in the art from the above description. Such modifications are also intended to fall within the scope of the appended claims.
    权利要求:
    Claims (34)
    [1]
    1. Process for preparing the compound of formula I:

    [2]
    2/8 where n is defined above.
    2. Process according to claim 1,
    CHARACTERIZED by the fact that n is 2 to 6 and R 1 , R 2 , R 3 and R 4 are hydrogen.
    [3]
    3. Process for preparing the compound of formula II:

    [4]
    4. Process, according to claim 1 or 3, CHARACTERIZED by the fact that the entrainer is present.
    [5]
    5. Process according to claim 1 or 3,
    CHARACTERIZED by the fact that the solvent is present.
    [6]
    6. Process according to claim 1 or 3,
    CHARACTERIZED by the fact that both the solvent and the entrainer are present.
    [7]
    7. Process according to claims 1 or 3, CHARACTERIZED by the fact that the catalyst is an alkyl halide, halides
    Petition 870180133795, of 9/24/2018, p. 13/31
    3/8 alkali, alkaline earth metal halides, transition metals and their halides or acid catalysts.
    [8]
    8. Process according to claim 1 or 3, CHARACTERIZED by the fact that the catalyst is sodium iodide, lithium bromide, lithium chloride, potassium iodide, potassium bromide, lithium iodide, C 1 alkyl iodide -C 6 , C 1 -C 6 alkyl bromide, 2-iodoethanol, 2-bromoethanol, 2-chloroethanol,
    3-iodopropanol, 3-bromopropanol, ferric bromide, ferrous chloride, ferrous bromide, manganese halide, copper powder, nickel halide, cobalt chloride, cesium bromide, palladium chloride, sulfuric acid, aryl sulfonic acid, alkyl acid sulfonic, aralkyl sulfonic acid, hydrochloric acid, hydrobromic acid, hydrofluoric acid, oxalic acid, perchloric acid, sulfonic trifluoromethane, fluorsulfonic acid, nitric acid, aluminum chloride, aluminum diethyl chloride, hydrogen chloride / aluminum triethyl, ferric chloride, zinc chloride, antimony trichloride, stannous chloride, boron trifluoride, acidic zeolites, acidic clays, polymeric sulfonic acids or mixtures thereof.
    [9]
    9. Process according to claim 5, CHARACTERIZED by the fact that the solvent is a solvent with a high boiling point, in which the solvent with a high boiling point has a boiling point greater than approximately 150 ° C in 1 atmosphere and melting point greater than approximately -100 ° C.
    [10]
    10. Process according to claim 9, CHARACTERIZED by the fact that the solvent with a high boiling point is diphenyl methane, diphenyl ethane, diphenyl propane, biphenyl, decahydronaphthalene, cyclohexyl benzene, 1,3-diisopropyl benzene, dimethyl sulfoxide ( DMSO), dimethyl formamide (DMF), dimethyl acetamide (DMAC), ethylene glycol dimethyl ether, ethylene glycol diethyl ether or mixtures thereof.
    [11]
    11. Process according to claim 5, CHARACTERIZED by the fact that the process is conducted at a pressure greater than approximately 1 atmospheric pressure and the solvent is a low boiling solvent having a boiling point less than approximately 150 ° C
    Petition 870180133795, of 9/24/2018, p. 14/31
    4/8 in 1 atmosphere.
    [12]
    12. Process according to claim 11, CHARACTERIZED by the fact that the solvent is heptane, hexane, petroleum ether, methyl cyclohexane; toluene, xylene, mesitylene, ethyl benzene, tetrahydrofuran, 1,4dioxane, acetonitrile or mixtures thereof.
    [13]
    13. Process according to claim 1 or 3, characterized by the fact that the reaction temperature varies from approximately 100 ° C to approximately 250 ° C.
    [14]
    14. Process according to claims 1 or 3,
    CHARACTERIZED by the fact that the process is carried out in a continuous way.
    [15]
    15. Process according to claim 1 or 3,
    CHARACTERIZED by the fact that the process is carried out in a batch mode.
    [16]
    16. Process according to claim 1 or 3, CHARACTERIZED by the fact that a reaction product is water and in which water and the diol compound of formula B or ethylene glycol are continuously recycled back to the reactor.
    [17]
    17. Process according to claim 6, CHARACTERIZED by the fact that the process is conducted at normal pressure and the entrainer is continuously recycled back to the reactor.
    [18]
    18. Process according to claim 1 or 3, CHARACTERIZED by the fact that the entrainer is a low-boiling solvent, wherein the low-boiling solvent has a lower boiling point than approximately 150 ° Ç.
    [19]
    19. Process according to claim 18, CHARACTERIZED by the fact that the low-boiling solvent is pentane, hexane, heptane, octane, cyclohexane, methyl cyclohexane, toluene, xylenes, ethyl benzene, isopropyl benzene or mixtures thereof .
    [20]
    20. Process according to claim 1 or 3, CHARACTERIZED by the fact that the catalyst is an acid catalyst.
    Petition 870180133795, of 9/24/2018, p. 15/31
    5/8
    [21]
    21. Process according to claim 20, CHARACTERIZED by the fact that the acid catalyst is sulfuric acid, aryl sulfonic acid, alkyl sulfonic acid, aralkyl sulfonic acid, hydrochloric acid, hydrobromic acid, hydrofluoric acid, oxalic acid, perchloric acid, trifluoromethane sulfonic acid, fluorsulfonic acid, nitric acid, phosphoric acid, phosphonic acids, phosphonic acids, aluminum chloride, diethyl aluminum chloride, hydrogen chloride / aluminum triethyl, ferric chloride, zinc chloride, antimony trichloride, trichloride, trifluoride boron, acidic zeolites, acidic clays, polymeric sulfonic acids or mixtures thereof.
    [22]
    22. Composition, CHARACTERIZED by the fact that it comprises the diastereomer of formula lia:

    [23]
    23. The composition according to claim 22,
    CHARACTERIZED by the fact that it also comprises enantiomers having the following formulas:

    [24]
    24. Composition according to claim 22, CHARACTERIZED by the fact that a plurality of compounds in the composition is the diastereomer of formula 11a.
    [25]
    25. Composition according to claim 22, CHARACTERIZED by the fact that it has an Isomer Ratio greater than 0.5 using the 3 IP NMR method.
    [26]
    26. Composition according to claim 22, CHARACTERIZED by the fact that it has an Isomer Ratio greater than 0.8 using the 3 IP NMR method.
    [27]
    27. Composition, according to claim 22, CHARACTERIZED by the fact that it has an Isomer Ratio greater than 0.95 using the 31PNMR method.
    [28]
    28. Process for producing a higher melting composition comprising the compound of formula II:

    [29]
    29. Composition according to claim 28, CHARACTERIZED by the fact that the acid catalyst is sulfuric acid, aryl acid
    Petition 870180133795, of 9/24/2018, p. 17/31
    7/8 sulfonic acid, alkyl sulfonic acid, aralkyl sulfonic acid, hydrochloric acid, hydrofluoric acid, oxalic acid, perchloric acid, trifluoromethane sulfonic acid, fluorsulfonic acid, nitric acid, phosphoric acid, phosphonic acids, phosphonic acids, aluminum chloride , diethyl aluminum chloride, hydrogen chloride / aluminum triethyl, ferric chloride, zinc chloride, antimony trichloride, stanic chloride, boron trifluoride, acidic zeolites, acidic clays, polymeric sulfonic acids or mixtures thereof.
    [30]
    30. Flame retardant polymer composition, CHARACTERIZED by the fact that it comprises a polymer and the compound of claim 22.
    [31]
    31. Composition according to claim 30, CHARACTERIZED by the fact that the polymer is polyolefins, polyesters, polyethers, polyketones, polyamides, polyvinyl chlorides, natural and synthetic rubbers, polyurethanes, polystyrenes, poly (meth) acrylates, phenolic resins , polybenzoxazine, polyacetals, polyacrylonitriles, polybutadienes, polystyrenes, polyimides, polyamideimides, polyetherimides, polyphenyl sulfides, polyphenylene oxide, polycarbonates, cellulose, cellulose derivatives, cyanate esters, polyphenylene esters, polyphenylene resins, resadine resins, resins butadiene-divinylbenzene-styrene resins, epoxy-modified polybutadiene resins, vinyl or acrylic acetate adhesives, carboxyl-terminated butadiene-acrylonitrile copolymers, phenylene ethers, butadiene-styrene copolymers grafted with maleic anhydride, 4-resin resins methyl-1 pentene modified by maleic anhydride, copolymers of 1-butene-ethylen o maleatados, resins derived from benzyl vinyl ether compounds, epoxy resins or mixtures thereof.
    [32]
    32. Composition, according to claim 30, CHARACTERIZED by the fact that the polymer is made of polyolefins, polyesters, phenolic resins, polyamides, polyurethanes, polystyrene, epoxy resins or mixtures thereof.
    [33]
    33. Composition according to claim 30, CHARACTERIZED by the fact that it also comprises a polyphosphate of
    Petition 870180133795, of 9/24/2018, p. 18/31
    8/8 melamine.
    [34]
    34. Composition according to claim 30,
    CHARACTERIZED by the fact that it still comprises silica.
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    法律状态:
    2018-06-12| B07A| Technical examination (opinion): publication of technical examination (opinion)|
    2018-06-26| B07C| Technical examination (opinion): republication|
    2019-12-10| B09A| Decision: intention to grant|
    2019-12-24| B25G| Requested change of headquarter approved|Owner name: ALBEMARLE CORPORATION (US) |
    2020-01-14| B25G| Requested change of headquarter approved|Owner name: ALBEMARLE CORPORATION (US) |
    2020-01-21| B16A| Patent or certificate of addition of invention granted|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 28/03/2011, OBSERVADAS AS CONDICOES LEGAIS. |
    优先权:
    申请号 | 申请日 | 专利标题
    US31958010P| true| 2010-03-31|2010-03-31|
    US41069410P| true| 2010-11-05|2010-11-05|
    PCT/US2011/030183|WO2011123389A1|2010-03-31|2011-03-28|Process for preparation of dopo-derived compounds and compositions thereof|
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