WO2002062808A1 - Process for purification of phosphate esters - Google Patents

Process for purification of phosphate esters Download PDF

Info

Publication number
WO2002062808A1
WO2002062808A1 PCT/US2002/003522 US0203522W WO02062808A1 WO 2002062808 A1 WO2002062808 A1 WO 2002062808A1 US 0203522 W US0203522 W US 0203522W WO 02062808 A1 WO02062808 A1 WO 02062808A1
Authority
WO
WIPO (PCT)
Prior art keywords
process according
epoxy
product
acid
phosphate ester
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/US2002/003522
Other languages
French (fr)
Inventor
Danielle Bright
Eric W. Burkhardt
Antoon Ten Kate
Sophia Dashevsky
John Tomko
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Akzo Nobel NV
Original Assignee
Akzo Nobel NV
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Akzo Nobel NV filed Critical Akzo Nobel NV
Priority to KR10-2003-7010209A priority Critical patent/KR20040060844A/en
Priority to DE60234679T priority patent/DE60234679D1/en
Priority to US10/467,262 priority patent/US7759522B2/en
Priority to AT02706170T priority patent/ATE451379T1/en
Priority to EP02706170A priority patent/EP1358193B1/en
Priority to JP2002563160A priority patent/JP2005502588A/en
Publication of WO2002062808A1 publication Critical patent/WO2002062808A1/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
    • C07F9/00—Compounds containing elements of Groups 5 or 15 of the Periodic Table
    • C07F9/02—Phosphorus compounds
    • C07F9/06—Phosphorus compounds without P—C bonds
    • C07F9/08—Esters of oxyacids of phosphorus
    • C07F9/09—Esters of phosphoric acids
    • C07F9/093—Polyol derivatives esterified at least twice by phosphoric acid groups
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
    • C07F9/00—Compounds containing elements of Groups 5 or 15 of the Periodic Table
    • C07F9/02—Phosphorus compounds
    • C07F9/025—Purification; Separation; Stabilisation; Desodorisation of organo-phosphorus compounds
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
    • C07F9/00—Compounds containing elements of Groups 5 or 15 of the Periodic Table
    • C07F9/02—Phosphorus compounds
    • C07F9/06—Phosphorus compounds without P—C bonds
    • C07F9/08—Esters of oxyacids of phosphorus
    • C07F9/09—Esters of phosphoric acids
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
    • C07F9/00—Compounds containing elements of Groups 5 or 15 of the Periodic Table
    • C07F9/02—Phosphorus compounds
    • C07F9/06—Phosphorus compounds without P—C bonds
    • C07F9/08—Esters of oxyacids of phosphorus
    • C07F9/09—Esters of phosphoric acids
    • C07F9/12—Esters of phosphoric acids with hydroxyaryl compounds

Definitions

  • the present invention is useful in the purification of phosphate ester compositions , in general , with aromatic oligomeric phosphate ester compositions being a preferred class of material for treatment.
  • aromatic oligomeric phosphates which are used as flame retardants for thermoplastic resins, are made by reaction of POCI 3 with a biphenol or a diol followed by reaction with phenol (or, alternatively, by reaction of diphenyl chlorophosphate with a biphenol) in the presence of a Lewis acid catalyst to form what is termed a "crude phosphate" composition.
  • a Lewis acid catalyst to form what is termed a "crude phosphate" composition.
  • catalyst residues for example, such metal species as magnesium, aluminum, zinc, and titanium
  • other acidic impurities that may negatively impact the properties of polymers (for example, polycarbonates , polyesters , and the like) to which the flame retardant is to be added.
  • chelating agent is intended to encompass those molecules and ions that can bond to a metal cation.
  • suitable chelating agent compositions for use herein include dilute acidic aqueous solutions that comprise an Arhenius acid, such as hydrochloric acid, phosphoric acid, carboxylic acids, a phosphonic acid, sulfuric acids, sulfonic acids , and the like .
  • solutions containing such chelating agent as ethylenediamine or ethylenediaminetetraacetic acid (EDTA) can also be employed.
  • the process herein involves washing the crude reaction product with such a chelating agent, followed, preferably, by one or two water washes to remove the catalyst.
  • the chelating agent is essential to effect the removal of Lewis acid catalyst residues (see Comparative Example 1) .
  • the chelating agent treatment preferably takes place at temperatures that range from about 40°C to about 90 °C using an amount of chelating agent, on an active basis, that ranges from about equimolar to about 100% over equimolar.
  • the use of temperatures near the upper limit of the aforementioned temperature range will result in a shorter time within which the desired reaction of chelating agent and metal occurs .
  • the use of the preferred water washes following the dilute chelating agent wash allow for removal of excess chelating agent from the phosphate ester oil, thereby contributing to a decrease in acidity (see, for example, Example 2, which follows).
  • the crude product is then preferably dried under reduced pressure, filtered and is then treated with an acid scavenger. Drying of the crude product prior to treatment with the acid scavenger is also important to the process of this invention since the presence of water impedes the action of the acid scavenger additive (see, for example, Example 9, which follows) .
  • Useful , representative acid scavengers are compounds containing epoxy groups.
  • suitable epoxy compounds that can be used in accordance with the present invention include ethylene oxid , propylene oxide , cyclohexene oxide, styrene oxide, epoxidized soybean oil, 3 , 4-epoxycyclohexyl-methyl-3 , 4-epoxy-cyclohexane- carboxylate, vinyl cyclohexene dioxide, 2- (3,4- epoxycyclohexyl-5 , 5-spiro-3, 4-epoxy) cyclohexane-meta- dioxane, bis (3,4-epoxycyclohexyl) adipate, 1,2-epoxy-p- vinylcyclohexene , Bisphenol A epoxy resins (for example, ARALDITE ® , a brand name of Ciba Specialty Chemicals) , and the like .
  • ARALDITE ® a brand name of Ciba Specialt
  • the number of equivalents of epoxy used be equal to or greater than the number of equivalents of acid present in the crude phosphate ester based on the Total Acid Number ("TAN") of the crude phosphate ester.
  • Total Acid Number is defined as the number of milligrams of potassium hydroxide required to neutralize one gram of sample, the determination of which is described in ASTM method D974.
  • the treatment with the acid scavenger can take place at temperatures that can range from about 25°C to about 200°C.
  • the amount of acid scavenger that is employed, on an actives basis can generally range from about stoichiometric amount to about 100% excess, based on the acid number.
  • Step 1 To 1200 g. of 0.4% oxalic acid in water, which was heated to 90°C with stirring, was added 1000 g. of the reaction mixture from Example 1. The mixture was agitated for thirty minutes and was allowed to separate. The acid number of the oil was 0.74 mg. KOH/g. The oil layer was washed twice with water at 65°C and was dried under vacuum to give 913.2 g. of product. The magnesium content of this product was 20 ppm, and the acid number was 0.48 mg. KOH/g.
  • Step 1 To 600.3 g. of 1% phosphoric acid in water, which was heated to 90°C with stirring, was added 503.8 g. of the reaction mixture from Example 1. The mixture was agitated for ninety minutes and was allowed to separate. The acid number of the oil was 0.45 mg. KOH/g. The oil layer was washed once with water at 65°C and was dried under vacuum to give 512.0 g. of product. The magnesium content of this product was 38 ppm, and the acid number was 0.28 mg. KOH/g.
  • Step 1 To 550 g. of 0.8% DEQUEST sequestrant 2010 (1- hydroxyethylidene-1-l-diphosphonic acid, from Solutia) in water, which was heated to 90°C with stirring, was added 445.8 g. of the reaction mixture from Example 1. The mixture was agitated for ninety minutes and was allowed to separate. The acid number of the oil was 1.22 mg. KOH/g. The oil layer was washed once with water at 65°C and was dried under vacuum to give 444.1 g. of product. The magnesium content of this product was 40 ppm, and the acid number was 0.29 mg. KOH/g.
  • Step 1 To 605.5 g. of 0.9% BAYHIBIT AM (2-Phosphono- 1,2,4-butane tricarboxylic acid, from Bayer) in water, which was heated to 90°C with stirring, was added 504.7 g. of the reaction mixture from Example 1. The mixture was agitated for ninety minutes and was allowed to separate. The acid number of the oil was 0.28 mg. KOH/g. The oil layer was washed once with water at 65°C and was dried under vacuum to give 504.7 g. of product. The magnesium content of this product was 11 ppm, and the acid number was 0.21 mg. KOH/g.
  • BAYHIBIT AM 2-Phosphono- 1,2,4-butane tricarboxylic acid, from Bayer
  • Step 1 To 705.0 g. of water, which was heated to 90°C with stirring, was added 614.7 g. of the reaction mixture from Example 1. The mixture was agitated or sixty minutes and was allowed to separate. The acid number of the oil was 1.1 mg. KOH/g. The oil layer was washed once more with water at 65°C and was dried under vacuum to give 599.1 g. of product. After filtration of the oil, the magnesium content of this product was 160 ppm, and the acid number was 0.58 mg. KOH/g.
  • the described mode of operation is batch, but the method is not restricted to batch operation. It can as well be performed in a continuous mode.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Biochemistry (AREA)
  • General Health & Medical Sciences (AREA)
  • Molecular Biology (AREA)
  • Fireproofing Substances (AREA)
  • Detergent Compositions (AREA)

Abstract

A crude phosphate ester product can be purified by first washing it with chelating agent composition (such as a dilute acidic solution) and then, preferably, water, drying the resulting product, and then treating the resulting product with an acid scavenger, as exemplified by an epoxy-containing compound, such as 3,4-epoxy cyclohexyl methyl-3,4-epoxy cyclohexyl carboxylate.

Description

Process for Purification of Phosphate Esters
The present invention is useful in the purification of phosphate ester compositions , in general , with aromatic oligomeric phosphate ester compositions being a preferred class of material for treatment.
For example, aromatic oligomeric phosphates, which are used as flame retardants for thermoplastic resins, are made by reaction of POCI3 with a biphenol or a diol followed by reaction with phenol (or, alternatively, by reaction of diphenyl chlorophosphate with a biphenol) in the presence of a Lewis acid catalyst to form what is termed a "crude phosphate" composition. Usually, extensive washing of this type of product is needed to remove catalyst residues (for example, such metal species as magnesium, aluminum, zinc, and titanium) and other acidic impurities that may negatively impact the properties of polymers (for example, polycarbonates , polyesters , and the like) to which the flame retardant is to be added.
In Examples 1 to 6 of U.S. Patent No. 5,616,768 to S. Kawata, such a reaction product is washed with an acidic aqueous solution to remove the catalyst and is then dried under reduced pressure . In Examples 1 to 14 of the same patent, the crude ester is treated with an epoxy compound at elevated temperature, washed with water, heated for a certain time and washed again with water. The oil layer is then dried under reduced pressure to give a purified product. This process is cumbersome and involves two wash and two drying sequences . The present invention is a new, simplified purification process to obtain a product of low metal content and low acidity. This new process comprises washing the reaction product with a dilute solution of a chelating agent. As used herein, the term "chelating agent" is intended to encompass those molecules and ions that can bond to a metal cation. Examples suitable chelating agent compositions for use herein include dilute acidic aqueous solutions that comprise an Arhenius acid, such as hydrochloric acid, phosphoric acid, carboxylic acids, a phosphonic acid, sulfuric acids, sulfonic acids , and the like . Also solutions containing such chelating agent as ethylenediamine or ethylenediaminetetraacetic acid (EDTA) can also be employed. The process herein involves washing the crude reaction product with such a chelating agent, followed, preferably, by one or two water washes to remove the catalyst. The chelating agent is essential to effect the removal of Lewis acid catalyst residues (see Comparative Example 1) . The chelating agent treatment preferably takes place at temperatures that range from about 40°C to about 90 °C using an amount of chelating agent, on an active basis, that ranges from about equimolar to about 100% over equimolar. The use of temperatures near the upper limit of the aforementioned temperature range will result in a shorter time within which the desired reaction of chelating agent and metal occurs .
The use of the preferred water washes following the dilute chelating agent wash allow for removal of excess chelating agent from the phosphate ester oil, thereby contributing to a decrease in acidity (see, for example, Example 2, which follows). The crude product is then preferably dried under reduced pressure, filtered and is then treated with an acid scavenger. Drying of the crude product prior to treatment with the acid scavenger is also important to the process of this invention since the presence of water impedes the action of the acid scavenger additive (see, for example, Example 9, which follows) .
Useful , representative acid scavengers are compounds containing epoxy groups. Examples of suitable epoxy compounds that can be used in accordance with the present invention include ethylene oxid , propylene oxide , cyclohexene oxide, styrene oxide, epoxidized soybean oil, 3 , 4-epoxycyclohexyl-methyl-3 , 4-epoxy-cyclohexane- carboxylate, vinyl cyclohexene dioxide, 2- (3,4- epoxycyclohexyl-5 , 5-spiro-3, 4-epoxy) cyclohexane-meta- dioxane, bis (3,4-epoxycyclohexyl) adipate, 1,2-epoxy-p- vinylcyclohexene , Bisphenol A epoxy resins (for example, ARALDITE®, a brand name of Ciba Specialty Chemicals) , and the like . In general , it is preferred that the number of equivalents of epoxy used be equal to or greater than the number of equivalents of acid present in the crude phosphate ester based on the Total Acid Number ("TAN") of the crude phosphate ester. Total Acid Number is defined as the number of milligrams of potassium hydroxide required to neutralize one gram of sample, the determination of which is described in ASTM method D974. The treatment with the acid scavenger can take place at temperatures that can range from about 25°C to about 200°C. The amount of acid scavenger that is employed, on an actives basis, can generally range from about stoichiometric amount to about 100% excess, based on the acid number. The Examples that follow illustrate this invention. Example 1: Synthesis of reaction mixture:
To 1249.2 g. of "DPCP mix" (this mixture contains mainly diphenyl chlorophosphate, "DPCP", and small amounts of monophenyl dichlorophosphate and triphenyl phosphate) and 4.2 g. of magnesium chloride, which was heated to 140°C under 50 mm vacuum, was continuously added 513 g. of bisphenol A over an eight hour period. At the end of this addition, the reaction mixture was held at 140°C for an additional three and one half-hours . The resulting crude phosphate ester had an acid number of 4.4 mg. KOH/g. The magnesium content of the crude product was 2600 ppm.
Example 2 : Purification of reaction mixture:
Step 1: To 1200 g. of 0.4% oxalic acid in water, which was heated to 90°C with stirring, was added 1000 g. of the reaction mixture from Example 1. The mixture was agitated for thirty minutes and was allowed to separate. The acid number of the oil was 0.74 mg. KOH/g. The oil layer was washed twice with water at 65°C and was dried under vacuum to give 913.2 g. of product. The magnesium content of this product was 20 ppm, and the acid number was 0.48 mg. KOH/g.
Step 2 : To the oil from step 1 of this Example (acid number = 0.48 mg. KOH/g) was added, with stirring at 65°C, 1.39 g. of 3,4-epoxy cyclohexyl methyl-3,4-epoxy cyclohexyl carboxylate, "ERL 4221" brand (a bis epoxide product available from Union Carbide) . After four hours, the acid number of the resulting Bisphenol A bis (diphenyl phosphate) product, "BDP", was 0.019 mg. KOH/g. Examples 3 to 5 , which follow, show alternative embodiments for practicing just step 1 of the purification of the reaction mixture that was previously exemplified.
Example 3 : Purification of reaction mixture :
Step 1: To 600.3 g. of 1% phosphoric acid in water, which was heated to 90°C with stirring, was added 503.8 g. of the reaction mixture from Example 1. The mixture was agitated for ninety minutes and was allowed to separate. The acid number of the oil was 0.45 mg. KOH/g. The oil layer was washed once with water at 65°C and was dried under vacuum to give 512.0 g. of product. The magnesium content of this product was 38 ppm, and the acid number was 0.28 mg. KOH/g.
Example 4 : Purification of reaction mixture :
Step 1: To 550 g. of 0.8% DEQUEST sequestrant 2010 (1- hydroxyethylidene-1-l-diphosphonic acid, from Solutia) in water, which was heated to 90°C with stirring, was added 445.8 g. of the reaction mixture from Example 1. The mixture was agitated for ninety minutes and was allowed to separate. The acid number of the oil was 1.22 mg. KOH/g. The oil layer was washed once with water at 65°C and was dried under vacuum to give 444.1 g. of product. The magnesium content of this product was 40 ppm, and the acid number was 0.29 mg. KOH/g.
Example 5 : Purification of reaction mixture :
Step 1: To 605.5 g. of 0.9% BAYHIBIT AM (2-Phosphono- 1,2,4-butane tricarboxylic acid, from Bayer) in water, which was heated to 90°C with stirring, was added 504.7 g. of the reaction mixture from Example 1. The mixture was agitated for ninety minutes and was allowed to separate. The acid number of the oil was 0.28 mg. KOH/g. The oil layer was washed once with water at 65°C and was dried under vacuum to give 504.7 g. of product. The magnesium content of this product was 11 ppm, and the acid number was 0.21 mg. KOH/g.
Examples 6 - 8, which follow, show alternative embodiments for practicing just step 2 of the purification of the reaction mixture.
Example 6 : Purification of reaction mixture
Step 2: To 1216 g. of crude BDP that was previously washed with oxalic acid and water as described in step 1 of Example 1 (acid number = 0.48 mg. KOH/g and magnesium content = 11 ppm) was added, with stirring at 110°C, 1.65 g. of 3,4-epoxy cyclohexyl methyl-3,4-epoxy cyclohexyl carboxylate, "ERL 4221" brand (a bisepoxide product available from Union Carbide) . After ninety minutes, the acid number of the resulting Bisphenol A bis (diphenyl phosphate) product, "BDP", was 0.017 mg. KOH/g.
Example 7 : Purification of reaction mixture
Step 2: To 1232 g. of crude BDP that was previously washed with oxalic acid and water as described in step 1 of Example 1 (acid number = 0.48 mg. KOH/g and magnesium content = 11 ppm) was added, with stirring at 130°C, 1.68 g. of 3,4-epoxy cyclohexyl methy1-3, 4-epoxy cyclohexyl carboxylate, "ERL 4221" brand (already described earlier. After 45 minutes , the acid number of the resulting Bisphenol A bis (diphenyl phosphate) product, "BDP", was 0.019 mg. KOH/g.
Example 8 : Purification of reaction mixture
Step 2: To 600 g. of crude BDP that was previously washed with oxalic acid and water as described in step 1 of Example 1 (acid number = 0.53 mg. KOH/g and magnesium content = 13 ppm) was added, with stirring at 65°C, 0.63 g. of propylene oxide. After six hours, the acid number of the resulting Bisphenol A bis (diphenyl phosphate) product, "BDP", was 0.054 mg. KOH/g.
Example 9 : Purification of reaction mixture
Step 2: To 1000 g. of crude resorcinol bis (diphenyl phosphate) , "RDP" , that was previously washed with oxalic acid and water as described in step 1 of Example 1 (acid number = 0.30 mg. KOH/g and magnesium content = 6 ppm) was added, with stirring at 70°C, 5.0 g. of 3,4-epoxy cyclohexyl methyl-3,4-epoxy cyclohexyl carboxylate, "ERL 4221" brand. After three hours, the acid number of the resulting Resorcinol bis (diphenyl phosphate) product, "RDP", was 0.014 mg. KOH/g.
Example 10 : Effect of water on acid reduction
In this Example, 250 g. of wet bisphenol A bis (diphenyl phosphate), "BDP", (no drying step after washing with oxalic acid and water; containing 4 - 5% water), having an acid number 0.19 mg. KOH/g., was treated with 0.1214 g. of "ERL 4221" bis epoxide at 65°C for four hours , producing a product having an acid number of 0.15 mg. KOH/g.
Comparative Example 1 : Effect of magnesium on acid reduction
Step 1: To 705.0 g. of water, which was heated to 90°C with stirring, was added 614.7 g. of the reaction mixture from Example 1. The mixture was agitated or sixty minutes and was allowed to separate. The acid number of the oil was 1.1 mg. KOH/g. The oil layer was washed once more with water at 65°C and was dried under vacuum to give 599.1 g. of product. After filtration of the oil, the magnesium content of this product was 160 ppm, and the acid number was 0.58 mg. KOH/g.
Step 2: To 507.4 g. of the oil from step 1 (acid number = 0.58 mg. KOH/g) was added, with stirring at 110°C, 1.71 g. of 3,4-epoxy cyclohexyl methyl-3, 4-epoxy cyclohexyl carboxylate, "ERL 4221" brand. After one hour, the acid number of the resulting bisphenol A bis (diphenyl phosphate) product, "BDP", was 0.238 mg. KOH/g. Addition of supplemental ERL 4221 bis epoxide at 110°C for one hour did not decrease the acid number .
The described mode of operation is batch, but the method is not restricted to batch operation. It can as well be performed in a continuous mode.
The foregoing Examples should not be construed in a limiting fashion since they merely relate to certain preferred embodiments of the present invention . The scope of protection desired is set forth in the Claims that follow.

Claims

We claim:
1. A process for purifying a crude phosphate ester product which comprises washing the crude product with a chelating agent composition and then, optionally, with water, drying the resulting product, and treating the resulting product with an acid scavenger.
2. A process according to Claim 1 in which the acid scavenger is an epoxy-containing compound.
3. A process according to Claim 2 in which the epoxy- containing compound is 3,4-epoxy cyclohexyl methyl-3, 4- epoxy cyclohexyl carboxylate.
4. A process according to Claim 1 in which washing with the chelating agent composition takes place at a temperature of from about 40°C to about 90°C
5. A process according to Claim 1 in which treatment with acid scavenger takes place at a temperature of from about 25°C to about 200°C
6. A process according to Claim 2 in which the number of equivalents of epoxy compound is equal to or greater than the number of equivalents of acid present in the crude phosphate ester based on the acid number of the crude phosphate ester.
7. A process according to Claim 1 in which the phosphate ester is heated with the epoxide at temperature ranging from about 40°C to about 200°C.
8. A process according to Claim 1 in which the phosphate ester is represented by the formula:
(ArO) 2-P (O) - [O-R-O-P (O) (OAr) -] n-OAr
where Ar is an aryl or alkaryl group, R is an arylene or alkylene group, and n is from 0 to 5.
9. A process according to Claim 6 where Ar is phenyl and
-0-R-O- is a bisphenol A moiety.
10. A process according to Claim 6 where Ar is phenyl and
-0-R-O- is a resorcinol moiety.
11. A process for purifying a crude phosphate ester product represented by the formula:
(ArO) 2-P (O) - [O-R-O-P (O) (OAr) -] „-OAr
where Ar is an aryl or alkaryl group, R is an arylene or alkylene group, and n is from 0 to 5 which comprises washing the crude product with an acidic aqueous solution and then optionally water, drying the resulting product, and treating the resulting product with an acid scavenger.
12. A process according to Claim 11 in which the acid scavenger is an epoxy-containing compound.
13. A process according to Claim 12 in which the acid scavenger is 3,4-epoxy cyclohexyl methyl-3, 4-epoxy cyclohexyl carboxylate .
PCT/US2002/003522 2001-02-08 2002-02-08 Process for purification of phosphate esters Ceased WO2002062808A1 (en)

Priority Applications (6)

Application Number Priority Date Filing Date Title
KR10-2003-7010209A KR20040060844A (en) 2001-02-08 2002-02-08 Process for purification of phosphate esters
DE60234679T DE60234679D1 (en) 2001-02-08 2002-02-08 PROCESS FOR CLEANING PHOSPHATE TESTERS
US10/467,262 US7759522B2 (en) 2001-02-08 2002-02-08 Process for purification of phosphate esters
AT02706170T ATE451379T1 (en) 2001-02-08 2002-02-08 METHOD FOR PURIFYING PHOSPHATE ESTERS
EP02706170A EP1358193B1 (en) 2001-02-08 2002-02-08 Process for purification of phosphate esters
JP2002563160A JP2005502588A (en) 2001-02-08 2002-02-08 Method for purifying phosphate ester

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US26725901P 2001-02-08 2001-02-08
US60/267,259 2001-02-08

Publications (1)

Publication Number Publication Date
WO2002062808A1 true WO2002062808A1 (en) 2002-08-15

Family

ID=23018008

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2002/003522 Ceased WO2002062808A1 (en) 2001-02-08 2002-02-08 Process for purification of phosphate esters

Country Status (8)

Country Link
US (1) US7759522B2 (en)
EP (1) EP1358193B1 (en)
JP (1) JP2005502588A (en)
KR (1) KR20040060844A (en)
CN (2) CN101307072A (en)
AT (1) ATE451379T1 (en)
DE (1) DE60234679D1 (en)
WO (1) WO2002062808A1 (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2004000922A1 (en) * 2002-06-25 2003-12-31 Akzo Nobel N.V. Low acidity phosphate esters
EP1554292A2 (en) * 2002-05-13 2005-07-20 Akzo Nobel N.V. Epoxy-stabilized polyphosphate compositions
WO2013048701A1 (en) * 2011-09-30 2013-04-04 Dow Technology Investments Llc Purification process

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101218272A (en) * 2005-03-03 2008-07-09 南达科他大豆处理机有限公司 Novel polyols derived from vegetable oils by oxidation
CN1884288B (en) * 2006-06-09 2012-06-13 四川花语精细化工有限公司 Process for manufacturing monoalkyl phosphate ester
CN101450953B (en) * 2008-12-30 2011-09-28 南京华狮化工有限公司 Method for preparing monoalkyl phosphoric acid esters and salt thereof
CN107793446A (en) * 2016-08-31 2018-03-13 天津市科密欧化学试剂有限公司 A kind of purification process of SILVER REAGENT tributyl phosphate
CN108752381A (en) * 2018-07-15 2018-11-06 程桂平 A kind of preparation method of biphosphonate

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4205023A (en) * 1978-10-02 1980-05-27 Stauffer Chemical Company Process for removing soluble metallic salts from a phosphate ester functional fluid
EP0690063A1 (en) * 1994-06-23 1996-01-03 Daihachi Chemical Industry Co., Ltd. Purification method of phosphoric esters

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3954917A (en) 1974-05-28 1976-05-04 Stauffer Chemical Company Method of preparing stable condensation products using an alcohol-alkylene oxide treatment and products therefrom
FR2374354A1 (en) 1976-12-17 1978-07-13 Revco Epoxy-cycloalkene derivs. used as acid scavenger - are esp. useful chlorinated solvent cleaning compsns. and halo-hydric acid-generating plastics e.g. PVC and chlorinated polyolefin
JP2901369B2 (en) 1991-01-30 1999-06-07 株式会社日立製作所 Refrigerator oil composition, refrigerant compressor and refrigeration device incorporating the same
JP3305165B2 (en) 1994-06-23 2002-07-22 大八化学工業株式会社 Method for purifying phosphates
JP3305228B2 (en) 1997-05-09 2002-07-22 大八化学工業株式会社 Method for producing phosphate ester compound
SG85605A1 (en) 1997-10-16 2002-01-15 Gen Electric Flame resistant compositions of polycarbonate and monovinylidene aromatic compounds
JP2000239285A (en) 1998-12-14 2000-09-05 Asahi Chem Ind Co Ltd Production of phosphate
JP2001002945A (en) 1999-06-23 2001-01-09 Asahi Chem Ind Co Ltd Stabilized flame retardant resin composition
JP4293748B2 (en) 1999-08-18 2009-07-08 大八化学工業株式会社 Method for purifying organophosphates
JP4518601B2 (en) 1999-11-05 2010-08-04 旭化成ケミカルズ株式会社 Flame retardant composition and method for producing resin composition using the same

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4205023A (en) * 1978-10-02 1980-05-27 Stauffer Chemical Company Process for removing soluble metallic salts from a phosphate ester functional fluid
EP0690063A1 (en) * 1994-06-23 1996-01-03 Daihachi Chemical Industry Co., Ltd. Purification method of phosphoric esters

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1554292A2 (en) * 2002-05-13 2005-07-20 Akzo Nobel N.V. Epoxy-stabilized polyphosphate compositions
WO2004000922A1 (en) * 2002-06-25 2003-12-31 Akzo Nobel N.V. Low acidity phosphate esters
US7442737B2 (en) 2002-06-25 2008-10-28 Supresta Llc Low acidity phosphate esters
WO2013048701A1 (en) * 2011-09-30 2013-04-04 Dow Technology Investments Llc Purification process

Also Published As

Publication number Publication date
KR20040060844A (en) 2004-07-06
EP1358193A1 (en) 2003-11-05
JP2005502588A (en) 2005-01-27
US20040116728A1 (en) 2004-06-17
DE60234679D1 (en) 2010-01-21
CN101307072A (en) 2008-11-19
CN1633441A (en) 2005-06-29
EP1358193B1 (en) 2009-12-09
US7759522B2 (en) 2010-07-20
CN100486979C (en) 2009-05-13
ATE451379T1 (en) 2009-12-15

Similar Documents

Publication Publication Date Title
EP2788284B1 (en) Mixtures of aluminium hydrogenphosphites with aluminium salts, process for the production thereof and the use thereof
US20110021803A1 (en) Purification and preparation of phosphorus-containing compounds
EP1358193B1 (en) Process for purification of phosphate esters
EP1327635B1 (en) Preparation of phenylphosphate esters of 4,4'-biphenol
US5616768A (en) Process for purifying phosphoric esters
US5457221A (en) Process for the manufacture of poly (hydrocarbylene aryl phosphate) compositions
JP2011132251A (en) Stable solution of rare earth tris (organophosphorus-derivative)
WO1998004566A1 (en) Process for the formation of hydrocarbyl bis(dihydrocarbyl phosphate)
JPS63210126A (en) Production of polycarbonate solution
JP3882750B2 (en) Purification of arylene polyphosphate esters
JPH08193089A (en) Method for producing phosphate ester
TWI709566B (en) Processes for producing organophosphorous compounds
JP4481246B2 (en) Epoxy stabilized polyphosphate composition
WO2011040287A1 (en) Processes for production of cyclic alkylene phosphohalidate and cyclic phosphoric acid ester
EP1516015B1 (en) Low acidity phosphate esters
KR20250147155A (en) Method for preparing bisphenol a bis(diphenyl phosphate), bisphenol a bis(diphenyl phosphate) prepared thereby, and flame retardant comprising the same
JP2007021286A (en) Treatment of wastewater containing organophosphorus compounds
KR100334999B1 (en) Process for separating phosphoric ester compound
KR20050062756A (en) Epoxy-stabilized polyphosphate compositions
JPH0242837B2 (en)
JP2004099526A (en) Method for producing pentaerythritol diphosphonate
KR20050024364A (en) Low acidity phosphate esters
MXPA01010803A (en) Stable solutions of rare earth tris (organophosphorus-derivatives)

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BY BZ CA CH CN CO CR CU CZ DE DK DM DZ EC EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NO NZ OM PH PL PT RO RU SD SE SG SI SK SL TJ TM TN TR TT TZ UA UG US UZ VN YU ZA

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): GH GM KE LS MW MZ SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG

121 Ep: the epo has been informed by wipo that ep was designated in this application
DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
WWE Wipo information: entry into national phase

Ref document number: 2002706170

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 1020037010209

Country of ref document: KR

WWE Wipo information: entry into national phase

Ref document number: 2002563160

Country of ref document: JP

WWE Wipo information: entry into national phase

Ref document number: 028047427

Country of ref document: CN

WWP Wipo information: published in national office

Ref document number: 2002706170

Country of ref document: EP

REG Reference to national code

Ref country code: DE

Ref legal event code: 8642

WWE Wipo information: entry into national phase

Ref document number: 10467262

Country of ref document: US

WWP Wipo information: published in national office

Ref document number: 1020037010209

Country of ref document: KR