|Title of Invention||
METHOD FOR REMOVAL OF ACETOL FROM PHENOL
|Abstract||A method is provided for the efficient, low cost removal of acetol from a phenol stream. The method results in removal of substantially all of the acetol from the phenol stream without the formation of substantial amounts of additional methylbenzofuran. The method also avoids the use of expensive reagents and capital intensive distillation equipment.|
METHOD FOR REMOVAL OF ACETOL FROM PHENOL
REFERENCE TO RELATED APPLICATIONS
 This application is a continuation-in-part of Application Serial Number
10/915,723 filed on August 9, 2004, and which claims priority under 35. U.S.C. § 119(e) to Provisional Patent Application Serial Number 60/556,236, which was filed on March 24, 2004.
FIELD OF THE INVENTION
 The present invention relates to the field of the production of high purity
phenol. More particularly, the present invention relates to the removal of acetol from phenol to obtain desired high purity.
BACKGROUND OF THE INVENTION
 The process commonly practiced for the production of phenol involves the
oxidation of cumene to cumene hydroperoxide, followed by its acid catalyzed decomposition to phenol and acetone. Isolation of phenol from the reaction product involves the neutralization of the acid catalyst, followed by a series of distillation and separation steps. The lower boiling components such as acetone, unreacted cumene as well as a-methylstyrene (AMS) are first recovered from the crude product by distillation. The remaining material is introduced into a phenol recovery column in which phenol is distilled away from the higher boiling impurities. Depending on the distillation procedures used to recover acetone, cumene and AMS, the distilled phenol may contain minor quantities of impurities such as mesityl oxide (MO), acetol (hydroxyacetone) and other aliphatic carbonyl compounds, olefinic compounds, acetophenone, cumylphenols and 2- and 3-methylbenzofuran (MBF) in addition to residual amounts of acetone, cumene and AMS. Such impurities are undesirable in phenol used in certain applications such as in the manufacture of bisphenol-A.
(0004] MBF is a particularly undesirable contaminant of phenol that is used for
certain applications such as in the production of bisphenol-A, a precursor to polycarbonate
resins. Due to similar volatility, MBF cannot be separated from phenol by fractional
distillation. U.S. Patents 5,064,507 and 4,857,151 describe a process of distillation in the
presence of water (also called steam stripping) to reduce MBF in phenol. However, due to
the high energy costs and the necessity to use large distillation columns, this process is
expensive in terms of capital investment and operating costs. U.S. Patent 5,414,154 describes
the use of a strong acid ion exchange resin to reduce the level of MBF by converting it to
higher boiling compounds. U.S. Patent 5,414,154 also showed that the effectiveness of MBF
removal by resin treatment increases with an increase in temperature.
 Although strong acid ion exchange resins also remove carbonyl compounds
from phenol on contact, acetol reacts with phenol to produce more MBF. U.S. Patent 5,414,154 teaches the necessity to remove acetol from phenol (e.g. by treatment with an amine) prior to contact with the resin to remove MBF.
 Although effective, amine treatment involves the use of an expensive reagent,
which must subsequently be purged from the phenol stream.
 Both U.S. Patents 3,810,946 and 6,489,519 disclose treatment of a phenol
stream containing acetol with an acid or acid resin to remove acetol. British Patent 0 865 677 discloses a process for removing acetol from a phenol stream wherein the phenol stream is heated in the presence or absence of a catalyst. However, in all of these patents, acetol is removed by reacting it with phenol to form MBF, which is subsequently purged from the phenol stream.
 European Patent 0 004 168 and U.S. Patent 4,857,151 disclose distillation
processes to remove acetol from phenol streams. However, these methods involve the use of capital intensive distillation apparatus.
 There remains a need for an efficient, low cost method for the removal of
acetol from a phenol stream that does not adversely affect phenol yields by formation of significant amount of additional MBF.
SUMMARY OF THE INVENTION
 The present invention provides efficient, low cost methodologies for the
removal of acetol from a phenol stream.
 In one embodiment of the present invention, a method for the efficient, low
cost removal of acetol from phenol comprises contacting a phenol stream containing acetol with an acidic resin at a temperature of about 85° C or less to convert acetol into higher boiling compounds other than methylbenzofuran. The phenol stream is then distilled to separate phenol from the higher boiling compounds.
 In another embodiment of the present invention, a method for the efficient,
low cost removal of acetol from phenol comprises of heating the phenol stream at a temperature greater than about 175°C to convert acetol into higher boiling compounds other than methylbenzofuran. This may be carried out with or without added alkali metal hydroxide. The phenol stream is then distilled to separate phenol from the higher boiling compounds.
 In both embodiments of the present invention, acetol is effectively removed
without reacting a large portion of the acetol with phenol, thus the present method results in reduced MBF formation and improved phenol yields.
BRIEF DESCRIPTION OF THE DRAWINGS
Figure 1- Illustrates the removal of acetol from a phenol stream by reaction with an acidic resin at 83° C.
Figure 2- Illustrates the removal of acetol from a phenol stream by reaction with an
acidic resin at 85° C and the absence of the formation of significant amounts of MBF on standing at 85° C.
Figure 3- Illustrates the formation of MBF that occurs when a phenol stream treated with acidic resin at 85°C is contacted directly with an acidic resin at 133° C
Figure 4- Illustrates the efficient removal of MBF from a phenol stream by reaction with an acidic resin at 134° C after acetol has been removed by a low temperature treatment with acid resin followed by distillation.
Figure 5- Illustrates the removal of acetol from a phenol stream by heating in a closed system at 198°C.
Figure 6- Illustrates the removal of acetol from a phenol stream by heating in a closed system at 198°C in the presence of 266ppm of 50% caustic.
DESCRIPTION OF THE INVENTION
 It has been discovered that acetol can be removed efficiently from phenol at a
low cost while minimizing the formation of methylbenzofuran (MBF). The treatment to remove acetol involves a treatment of distilled phenol containing acetol with either an acidic resin at low temperature or at elevated temperature, optionally with a small amount of caustic. By this treatment, acetol present in the crude phenol is converted primarily to high boiling products other than MBF. These high boiling products can then be separated from phenol via distillation.
 The removal of acetol is key to the subsequent efficient removal of MBF from
the crude phenol. As is known, at the high temperatures and acidic conditions used to convert MBF to products separable from phenol, acetol reacts with phenol to produce more MBF. This reaction has the dual effect of reducing phenol recovery and making the removal of MBF from the product less efficient.
 In one embodiment of the invention, a distilled phenol stream containing
acetol is contacted with an acidic resin at a temperature of about 85° C or less to convert acetol to higher boiling compounds other than MBF. Following the acidic resin treatment, phenol is separated from the higher boiling compounds by distillation. Treatment time and temperature will vary based on the quantity of acetol to be removed from the crude phenol. Treatment times can vary from 5 minutes to 1 hour. In an exemplary treatment 700 ppm of acetol was removed from a crude phenol stream by contacting with an acidic resin at a temperature of about 85° C for about 15 minutes. Only about 12% of the acetol in this example was converted into MBF.
 It is preferred that the acidic resin be in the form of a fixed bed, over which the
phenol stream is passed. The phenol stream is preferably passed over the resin bed at a rate of from 1 to 12 bed volumes per hour.
 Figure 1 shows the rapid reduction of acetol in a sample of phenol from
about 225 ppm by weight to near 0 ppm on treatment with Amberlyst 36 at 83 ° C. Note that the formation of MBF is minimal. If all of the acetol were to be converted to MBF, a total concentration of about 400 ppm by weight of MBF would be expected. Instead, the combined concentration of 2-MBF and 3-MBF is only about 25 ppm by weight. Figure 2 again shows the treatment of a crude phenol stream containing about 225 ppm by weight of acetol at 85° C with Amberlyst 36. Again, the reduction in acetol content to near 0 ppm is extremely rapid, with a minimal formation of MBF. As can further be seen in Figure 2, the
extended hold time at 85° C does not result in an increase in the content of MBF. This indicates that the heavy products produced from acetol by the acid resin treatment are stable at that temperature.
 The distillation following the acid resin treatment is preferably a flash
distillation performed at reduced pressure to avoid the formation of MBF that would result from the breakdown of high molecular weight species formed during the acid treatment. The use of a flash distillation under vacuum has the added advantage of eliminating costly distillation apparatus used to separate phenol and acetol in prior art methods. It will be recognized however, that various distillation methods can be used in conjunction with the invention as long as care is taken to avoid decomposition of the high molecular weight species formed during the acid treatment.
 Referring to Figure 3, the necessity of avoiding the decomposition of the
heavy products formed during the acid resin treatment is illustrated. Figure 3 shows the
effect of a high temperature resin treatment on a phenol stream that has been treated by acidic
resin at 85° C to convert acetol to higher boiling compounds, without first removing the
higher boiling products. As can be seen, the elevated temperature resulted in the formation of
additional MBF. This indicates that the higher boiling compounds formed in the low
temperature acidic resin treatment are decomposing back to acetol at high temperature in the
presence of the acidic resin, and then reacting with phenol to form MBF. Not only does this
result in a loss of phenol, but as can be seen, the time necessary to reduce the MBF content to
near 0 ppm by weight is extended significantly, approximately 130 minutes.
 Figure 4 illustrates an example where the higher boiling compounds formed
by treatment with acidic resin are removed by flash distillation of the phenol prior to acidic resin treatment at elevated temperature to remove MBF. As can be seen in Figure 4, no
increase in MBF content is experienced. Further, the MBF content is reduced to near 0 ppm in about 10 minutes, as opposed to 130 minutes.
 In an alternative embodiment of the invention, a distilled phenol stream
containing acetol is heated in a closed system at elevated temperature to convert acetol to higher boiling compounds other than MBF. The heat treatment may be carried out with or without the addition of a small amount of caustic. If the heat treatment is carried out without the addition of caustic, the pH of the phenol stream should be above 2, preferably above 2.5. In general, this is the pH of the distilled phenol stream from the neutralized reaction product. Lower pH may lead to additional amounts of MBF. The caustic is preferably added as a concentrated solution, e.g. 50 percent by weight. Again, the phenol is separated from the higher boiling compounds via distillation. The temperatures used for the heat treatment will be at least 175 to 225° C. The treatment time, temperature and the amount of caustic used (if required) will vary based on the quantity of acetol to be removed from the phenol stream. As illustrated in Figure 5, in an exemplary treatment 1036ppm of acetol was reduced to less than 10 ppm by heating at 198°C for about 4 hours without the addition of any caustic. In this example only 1 percent of the acetol was converted into MBF. As illustrated in Figure 6, in the presence of 266ppm of 50% caustic, 1045ppm of acetol was reduced to less than lOppm in only about 2 hours. However, a slightly higher amount of acetol (~1.6%) was converted into MBF. It should be pointed out that the efficient removal of acetol at elevated temperatures requires a low water content in the phenol stream being treated, for example less than 1.5 percent based on phenol. Preferably, the water content is reduced to about 0.1 percent by weight. Various methods for reducing the water content of organic streams, and phenol in particular, are known in the art. Other examples reducing acetol from 1800 ppm are shown in Table 1 below.
 Following the treatment to remove acetol, the phenol is distilled from the
higher boiling compounds, and can be passed to an acidic resin treatment at elevated temperature to remove MBF, as disclosed in U.S. Patents 5,414,154 and 6,388,144 B1, both of which are incorporated herein by reference in their entirety.
 The present method to remove acetol from phenol has the advantage of being
more cost efficient than prior art methods that involved the use of distillation apparatus, such as super splitter columns and prior art methods that used expensive amines. In addition, the present method has the advantage of producing less MBF from the acetol being removed, than other prior art methods, which utilized high concentrations of caustic or relied on multiple high temperature treatments with acidic resins.
What is claimed is
1. A process for removing acetol from a phenol stream, said method comprising:
providing a phenol stream containing acetol and having a water content of 1.5 weight percent or less based on phenol,
heating said phenol stream at a temperature of greater than about 175° C to convert acetol into higher boiling compounds other than methylbenzofuran, and
distilling said phenol stream to separate phenol from said higher boiling compounds.
2. The process according to claim 1, wherein an alkali metal hydroxide is added to the phenol stream to obtain an alkali metal concentration of 600 ppm by weight or less based on phenol.
3. The process according to claim 2 wherein said alkali metal hydroxide is sodium hydroxide.
4. The process of claim 1, wherein the phenol stream is heated to a temperature about 175°C to about 225°C.
The process of claim 2 wherein said phenol stream contains up to 1800 ppm acetol.
6. The process of claim 1, wherein said distillation is a flash distillation.
7. The process according to claim 1, wherein said heating is carried out for a period of about 2 to about 8 hours.
8. The method according to claim 1, wherein said phenol stream containing acetol is
treated to reduce the content of water in said phenol stream to 1.5 percent by weight or less
based on phenol prior to said adding of an alkali metal hydroxide.
9. The process according to claim 8, wherein said phenol stream is treated to reduce the
content of water to 0.1 percent by weight or less based on phenol prior to said adding of an
alkali metal hydroxide.
588-CHENP-2007 AMANDED CLAIMS 05-02-2010.pdf
588-CHENP-2007 AMANDED PAGES OF SPECIFICATION 05-02-2010.pdf
588-CHENP-2007 CORRESPONDENCE OTHERS 05-02-2010.pdf
588-chenp-2007 form-1 21-04-2010.pdf
588-CHENP-2007 FORM-2 21-04-2010.pdf
588-CHENP-2007 FORM-3 05-02-2010.pdf
588-CHENP-2007 FORM-6 21-04-2010.pdf
588-chenp-2007 power of attorney 21-04-2010.pdf
588-CHENP-2007 POWER OF ATTORNEY 12-03-2010.pdf
588-CHENP-2007 CORRESPONDENCE OTHERS 22-2-2010.pdf
588-chenp-2007 form-3 22-2-2010.pdf
588-CHENP-2007 OTHER PATENT DOCUMENT 22-2-2010.pdf
|Indian Patent Application Number||588/CHENP/2007|
|PG Journal Number||14/2010|
|Date of Filing||09-Feb-2007|
|Name of Patentee||SUNOCO, INC. (R&M)|
|Applicant Address||1735 MARKET STREET, PHILADELPHIA, PENNSYLVANIA 19103, USA|
|PCT International Classification Number||C07C 37/86|
|PCT International Application Number||PCT/US05/03228|
|PCT International Filing date||2005-02-03|