WO2004076389A1 - Process for the preparation of styrene - Google Patents

Process for the preparation of styrene Download PDF

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Publication number
WO2004076389A1
WO2004076389A1 PCT/EP2004/050191 EP2004050191W WO2004076389A1 WO 2004076389 A1 WO2004076389 A1 WO 2004076389A1 EP 2004050191 W EP2004050191 W EP 2004050191W WO 2004076389 A1 WO2004076389 A1 WO 2004076389A1
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Prior art keywords
catalyst
phenylethanol
styrene
dehydration
alumina
Prior art date
Application number
PCT/EP2004/050191
Other languages
French (fr)
Inventor
Johannes Adrianus Maria Van Broekhoven
Carolus Matthias Anna Maria Mesters
Original Assignee
Shell Internationale Research Maatschappij B.V.
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Application filed by Shell Internationale Research Maatschappij B.V. filed Critical Shell Internationale Research Maatschappij B.V.
Priority to JP2006502045A priority Critical patent/JP2006518723A/en
Priority to BRPI0407780-6A priority patent/BRPI0407780B1/en
Priority to AU2004215663A priority patent/AU2004215663B2/en
Priority to DE602004028577T priority patent/DE602004028577D1/en
Priority to AT04713902T priority patent/ATE477226T1/en
Priority to EP04713902A priority patent/EP1597216B1/en
Publication of WO2004076389A1 publication Critical patent/WO2004076389A1/en

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
    • B01J21/04—Alumina
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
    • C07C1/24—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms by elimination of water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/61—Surface area
    • B01J35/613—10-100 m2/g
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/61—Surface area
    • B01J35/615—100-500 m2/g
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/63—Pore volume
    • B01J35/635—0.5-1.0 ml/g
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
    • C07C2521/02—Boron or aluminium; Oxides or hydroxides thereof
    • C07C2521/04—Alumina

Definitions

  • the present invention relates to a process for the preparation of styrene comprising the gas phase dehydration of 1-phenylethanol at elevated temperature in the presence of a dehydration catalyst.
  • a commonly known method for manufacturing styrene is the coproduction of propylene oxide and styrene starting from ethylbenzene.
  • such process involves the steps of (i) reacting ethylbenzene with oxygen or air to form ethylbenzene hydroperoxide, (ii) reacting the ethylbenzene hydroperoxide thus obtained with propene in the presence of an epoxidation catalyst to yield propylene oxide and 1-phenylethanol (also known as ⁇ -phenylethanol or ethylphenylcarbinol) , and (iii) converting the 1-phenylethanol into styrene by dehydration using a suitable dehydration catalyst.
  • 1-phenylethanol also known as ⁇ -phenylethanol or ethylphenylcarbinol
  • US-A-3, 526, 674 discloses the use of an alumina catalyst in the liquid phase dehydration of 1-phenylethanol into styrene, wherein said alumina catalyst suitably has a BET surface area of 40 to 250 m.2/g and is used in finely divided form, i.e. in the form of particles having a particle size of 0.15 mm (100 mesh) or less.
  • US-A-3, 658, 928 discloses a process for the gas phase dehydration of 1-phenylethanol into styrene in the presence of controlled amounts of added steam and in the presence of a catalyst, which suitably is a commercially available alumina catalyst like Harshaw Al-0104. Harshaw Al-0104 catalyst has a pore volume of about 0.35 ml/g.
  • a dehydration process using alumina (aluminium oxide: A1 2 0 3 ) catalysts especially suitable for such process has been disclosed in WO 99/58480. Use of these catalysts allows advantageous conversion of 1-phenylethanol into styrene without many of the disadvantages of the use of prior art catalysts.
  • styrene also embraces substituted styrenes, by which are meant styrenes containing one or more substituents bonded to the aromatic ring or to the vinyl group.
  • substituents typically include alkyl groups, such as methyl or ethyl groups.
  • 1-phenylethanol also embraces substituted 1-phenyl- ethanols having the same substituents as the corresponding substituted styrenes .
  • an alumina dehydration catalyst wherein the catalyst has a BET surface area of from 80 to 140 m 2 /g and a pore volume (Hg) of more than 0.65 ml/g is suitable for the preparation of styrene by a gas phase dehydration of 1-phenylethanol at elevated temperature while the 1-phenylethanol dehydration was maintained at a high level for a long time. Additionally, it was found that such process produced less heavy by-products than prior art catalysts.
  • the pore volume (Hg) of the catalyst for use in the present invention is more than 0.65 ml/g.
  • the pore volume is at most 1.0 ml/g.
  • the catalyst preferably has a pore volume (Hg) of from 0.75 to 0.85 ml/g.
  • the BET surface area can be measured in any way known to be suitable to someone skilled in the art.
  • the expression pore volume (Hg) stands for the pore volume as measured with the help of mercury. Suitable methods for measuring the porosity with the help of mercury are also well known to someone skilled in the art.
  • Shaped alumina catalysts with the properties required for use in this invention can be prepared by procedures well known in the art, for example by extrusion of alumina or alumina precursor pastes, followed by calcination.
  • alumina precursors are alumina hydrates like aluminium oxide trihydrate, AI2O3.3H2O (also known as gibbsite or bayerite) and aluminium hydroxide A100H (also known as boehmite or pseudo-boehmite) . These alumina precursors are transformed to alumina during the calcination process.
  • alumina powder or alumina precursor powder is first optionally mixed with a binder powder.
  • Suitable binder materials include inorganic oxides like oxides of silicon, magnesium, titanium, aluminium, zirconium, and silicon-aluminium.
  • the weight ratio of binder to alumina powders may be from 0 (no binder present) up to 90:10.
  • an extrudable mixture is prepared from the solids (alumina powders and optionally binder) and water by mixing and kneading the ingredients and passing this mixture into the extruder.
  • Such extrudable mixture typically has a paste-like appearance. It is within the normal skills of those skilled in the art to optimize the mixing/kneading procedure to obtain an extrudable paste and to select the most appropriate extrusion conditions.
  • the extrusion paste will normally also comprise extrusion aids to improve the extrusion process.
  • extrusion aids include, for instance, peptizing agents and flocculating agents.
  • Peptizing agents facilitate a more dense packing of the particles in the extrusion mixture, while flocculating agents promote the inclusion of water.
  • Suitable peptizing agents include monovalent inorganic acids (e.g. hydrochloric acid and nitric acid) and organic acids such as aliphatic monocarboxylic acids, acyclic monocarboxylic acids, and fatty acids.
  • Suitable flocculating agents are also well known and include polyelectrolytes like those commercially available under the trade names NALCO and SUPERFLOC. Burnout materials may also be used to increase the porosity of the final extrudate. Examples of burnout materials are polyethylene oxide, methylcellulose, ethyl- cellulose, latex, starch, nut shells or flour, poly- ethylene or any of the polymeric microspheres or micro- waxes .
  • a catalyst particularly suitable for use in this invention can be made from pseudo-boehmite (AIOOH) .
  • AIOOH pseudo-boehmite
  • Such powder is commercially available from Criterion Catalyst Company .
  • the extrudable mixture or paste obtained as described above is then subjected to an extrusion treatment.
  • This extrusion treatment can be performed by conventional extrusion techniques known in the art.
  • an orifice is present, which gives the extruded mixture the selected shape when leaving the extruder.
  • the wet extrudate is first spheronized in a suitable spheronizing device after having left the extruder before being subjected to calcination.
  • the catalyst particles may have any shape, including spherical, cylindrical, trilobal, quadrulobal, star- shaped, ring-shaped, cross-shaped etc.
  • the green extrudates obtained as described above are then optionally dried and subsequently subjected to a calcination step.
  • a catalyst of the desired properties could be obtained by drying extrudates at temperatures of from 100 to 140 °C for several hours and thereafter calcining at high temperature for several hours.
  • the dehydration of 1-phenylethanol into styrene according to the present invention is carried out in the gas phase at elevated temperature.
  • elevated temperature preferably is any temperature above 150 °C.
  • the preferred dehydration conditions to be applied are those normally applied and include reaction temperatures of from 210 to 330 °C, more preferably of from 280 to 320 °C, and most preferably about 300 °C, and pressures in the range of from 0.1 to 10 bar, most preferably about 1 bara.
  • reaction selectivity is defined as the number of moles of styrene formed per mole of precursor compounds converted to products .
  • selectivities to other compounds such as heavy-ends are defined as the number of moles of precursor compounds to heavy-ends per mole of precursor compounds converted to products.
  • Conversion is defined as the overall conversion level ' of 1-phenylethanol as determined under test conditions, i.e.
  • the mole percentage of 1-phenylethanol converted relative to the total number of moles of 1-phenylethanol present in the feed is very low: selectivity towards ethers typically is less than 0.8%, more suitably less than 0.3%, whereas selectivity towards oligomers typically is less than 3% and preferably 2% or less.
  • a trilobe-shaped catalyst having the physical properties as indicated in Table I (Ex-1) was tested for dehydration performance in a microflow unit consisting of a 13 mm diameter plugflow reactor, 1-phenylethanol feed vaporization facilities and product vapour condensing facilities.
  • 1-phenylethanol feedstock was used a sample of the process stream to the styrene reactor system of a commercial Propylene Oxide/Styrene Monomer plant.
  • the feedstock contained 81.2% of 1-phenylethanol, 10.6% of methylphenylketone and 2% of water.
  • the remainder up to 100% consisted of impurities and (by) products of the preceding oxidation and epoxidation sections.
  • the outlet stream of the micro flow unit was liquefied by condensation and the resulting two-phase liquid system was analyzed by means of gas chromatographic analysis.
  • the dehydration experiment was carried out at test conditions of 1.0 bara pressure and a temperature of 300 °C.
  • the feed rate of 1-phenylethanol was maintained at 30 grams per hour and the reactor tube was loaded with 20 cm3 of catalyst.
  • the reaction was continued for approximately 140 hours after which the experiment was stopped.
  • Example 1 The procedure as described in Example 1 was repeated, except that a different sample of feedstock containing 81.3% of 1-phenylethanol and 9.9% of methylphenylketone was used. Data are reported in Table 1 (Ex-2) . Comparison Example 1
  • Example 1 The procedure as described in Example 1 was repeated, except that the trilobe-shaped catalyst had a BET surface area of 149 m ⁇ . Physical properties are indicated in Table 1 (Comp-Ex-1) . Only 1-phenylethanol conversion was monitored during the experiment, which was terminated after 98 hours, when 1-phenylethanol conversion was only
  • Example 2 The procedure as described in Example 1 was repeated, except that a star-shaped catalyst with physical properties within the ranges as described in the process according to WO 99/58480 was used. The reaction was continued for approximately 120 hours. Activity and selectivity data are given in Table 1 (Comp-Ex-2) . Comparison Example 3
  • Example 2 The procedure as described in Example 1 was repeated, except that a trilobe-shaped catalyst with physical properties within the ranges as described in the process according to WO 99/58480 was used. A sample of feedstock containing 79.0% of 1-phenylethanol and 10.0% of methylphenylketone was used. Data are reported in Table 1 (Comp-Ex-3) . The experiment was terminated after 113 hours, when 1-phenylethanol conversion was only 91%. Activity and selectivity data are given in Table 1 (Comp-Ex-3) .

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Epoxy Compounds (AREA)

Abstract

Process for the preparation of styrene comprising the gas phase dehydration of 1-phenylethanol at elevated temperature in the presence of a dehydration catalyst in which the dehydration catalyst comprises shaped alumina catalyst particles having a surface area (BET) of from 80 to 140 M2/g and a pore volume (Hg) of more than 0.65 ml/g.

Description

PROCESS FOR THE PREPARATION OF STYRENE
The present invention relates to a process for the preparation of styrene comprising the gas phase dehydration of 1-phenylethanol at elevated temperature in the presence of a dehydration catalyst.
A commonly known method for manufacturing styrene is the coproduction of propylene oxide and styrene starting from ethylbenzene. In general such process involves the steps of (i) reacting ethylbenzene with oxygen or air to form ethylbenzene hydroperoxide, (ii) reacting the ethylbenzene hydroperoxide thus obtained with propene in the presence of an epoxidation catalyst to yield propylene oxide and 1-phenylethanol (also known as α-phenylethanol or ethylphenylcarbinol) , and (iii) converting the 1-phenylethanol into styrene by dehydration using a suitable dehydration catalyst.
The use of alumina catalysts in the dehydration of 1-phenylethanol per se is well known in the art.
For instance, US-A-3, 526, 674 discloses the use of an alumina catalyst in the liquid phase dehydration of 1-phenylethanol into styrene, wherein said alumina catalyst suitably has a BET surface area of 40 to 250 m.2/g and is used in finely divided form, i.e. in the form of particles having a particle size of 0.15 mm (100 mesh) or less.
US-A-3, 658, 928 discloses a process for the gas phase dehydration of 1-phenylethanol into styrene in the presence of controlled amounts of added steam and in the presence of a catalyst, which suitably is a commercially available alumina catalyst like Harshaw Al-0104. Harshaw Al-0104 catalyst has a pore volume of about 0.35 ml/g. A dehydration process using alumina (aluminium oxide: A1203) catalysts especially suitable for such process has been disclosed in WO 99/58480. Use of these catalysts allows advantageous conversion of 1-phenylethanol into styrene without many of the disadvantages of the use of prior art catalysts. However, even use of these improved catalysts still leads to the formation of heavy by-products, typically up to 5% of oligomers and polymers of styrene. These heavy byproducts do not further convert and therefore decrease the overall yield of desired styrene. Furthermore, these high-molecular weight by-products tend to occupy the pores of the catalyst, after which the catalyst cannot longer be used for converting 1-phenylethanol into styrene. This necessitates a regeneration step of the catalyst, which unfavourably adds to the costs of the process.
It is therefore an object of the present invention to find a catalyst for the gas phase dehydration of 1- phenylethanol into styrene, wherein styrene is obtained at improved selectivity and 1-phenylethanol conversion can be maintained at a high level for a longer time. This means that the catalyst needs to be regenerated less frequently.
Within the context of the present application the term "styrene" also embraces substituted styrenes, by which are meant styrenes containing one or more substituents bonded to the aromatic ring or to the vinyl group. Such substituents typically include alkyl groups, such as methyl or ethyl groups. Similarly, the term "1-phenylethanol" also embraces substituted 1-phenyl- ethanols having the same substituents as the corresponding substituted styrenes .
It was found that an alumina dehydration catalyst wherein the catalyst has a BET surface area of from 80 to 140 m2/g and a pore volume (Hg) of more than 0.65 ml/g is suitable for the preparation of styrene by a gas phase dehydration of 1-phenylethanol at elevated temperature while the 1-phenylethanol dehydration was maintained at a high level for a long time. Additionally, it was found that such process produced less heavy by-products than prior art catalysts.
The pore volume (Hg) of the catalyst for use in the present invention is more than 0.65 ml/g. Preferably, the pore volume is at most 1.0 ml/g. More specifically, the catalyst preferably has a pore volume (Hg) of from 0.75 to 0.85 ml/g.
The BET surface area can be measured in any way known to be suitable to someone skilled in the art. The expression pore volume (Hg) stands for the pore volume as measured with the help of mercury. Suitable methods for measuring the porosity with the help of mercury are also well known to someone skilled in the art.
Shaped alumina catalysts with the properties required for use in this invention can be prepared by procedures well known in the art, for example by extrusion of alumina or alumina precursor pastes, followed by calcination. Examples of alumina precursors are alumina hydrates like aluminium oxide trihydrate, AI2O3.3H2O (also known as gibbsite or bayerite) and aluminium hydroxide A100H (also known as boehmite or pseudo-boehmite) . These alumina precursors are transformed to alumina during the calcination process. Typically, in such a process, alumina powder or alumina precursor powder is first optionally mixed with a binder powder. Suitable binder materials include inorganic oxides like oxides of silicon, magnesium, titanium, aluminium, zirconium, and silicon-aluminium. The weight ratio of binder to alumina powders may be from 0 (no binder present) up to 90:10. Typically an extrudable mixture is prepared from the solids (alumina powders and optionally binder) and water by mixing and kneading the ingredients and passing this mixture into the extruder. Such extrudable mixture typically has a paste-like appearance. It is within the normal skills of those skilled in the art to optimize the mixing/kneading procedure to obtain an extrudable paste and to select the most appropriate extrusion conditions. Besides the alumina, optional binder and water, the extrusion paste will normally also comprise extrusion aids to improve the extrusion process. Such extrusion aids are known in the art and include, for instance, peptizing agents and flocculating agents. Peptizing agents facilitate a more dense packing of the particles in the extrusion mixture, while flocculating agents promote the inclusion of water. Suitable peptizing agents are known in the art and include monovalent inorganic acids (e.g. hydrochloric acid and nitric acid) and organic acids such as aliphatic monocarboxylic acids, acyclic monocarboxylic acids, and fatty acids. Suitable flocculating agents are also well known and include polyelectrolytes like those commercially available under the trade names NALCO and SUPERFLOC. Burnout materials may also be used to increase the porosity of the final extrudate. Examples of burnout materials are polyethylene oxide, methylcellulose, ethyl- cellulose, latex, starch, nut shells or flour, poly- ethylene or any of the polymeric microspheres or micro- waxes .
A catalyst particularly suitable for use in this invention can be made from pseudo-boehmite (AIOOH) . Such powder is commercially available from Criterion Catalyst Company .
The extrudable mixture or paste obtained as described above is then subjected to an extrusion treatment. This extrusion treatment can be performed by conventional extrusion techniques known in the art. At the outlet of the extruder an orifice is present, which gives the extruded mixture the selected shape when leaving the extruder. When aiming to obtain spherically shaped extrudates, the wet extrudate is first spheronized in a suitable spheronizing device after having left the extruder before being subjected to calcination. The catalyst particles may have any shape, including spherical, cylindrical, trilobal, quadrulobal, star- shaped, ring-shaped, cross-shaped etc. The green extrudates obtained as described above are then optionally dried and subsequently subjected to a calcination step. A catalyst of the desired properties could be obtained by drying extrudates at temperatures of from 100 to 140 °C for several hours and thereafter calcining at high temperature for several hours.
The dehydration of 1-phenylethanol into styrene according to the present invention is carried out in the gas phase at elevated temperature. The term "elevated temperature" preferably is any temperature above 150 °C. The preferred dehydration conditions to be applied are those normally applied and include reaction temperatures of from 210 to 330 °C, more preferably of from 280 to 320 °C, and most preferably about 300 °C, and pressures in the range of from 0.1 to 10 bar, most preferably about 1 bara.
In the process according to the present invention the catalyst described hereinbefore was observed to have a reaction selectivity to styrene of at least 96% at a conversion of at least 99%, whilst selectivities of 97% or higher at conversions of 99% and higher have been achieved. In this connection, reaction selectivity is defined as the number of moles of styrene formed per mole of precursor compounds converted to products . Similarly, selectivities to other compounds such as heavy-ends are defined as the number of moles of precursor compounds to heavy-ends per mole of precursor compounds converted to products. Conversion is defined as the overall conversion level ' of 1-phenylethanol as determined under test conditions, i.e. the mole percentage of 1-phenylethanol converted relative to the total number of moles of 1-phenylethanol present in the feed. Furthermore, the selectivity of the catalyst towards heavy by-products like oligomers and ethers is very low: selectivity towards ethers typically is less than 0.8%, more suitably less than 0.3%, whereas selectivity towards oligomers typically is less than 3% and preferably 2% or less.
The invention will now be illustrated by the following examples without limiting the scope of the invention to these particular embodiments. Example 1
A trilobe-shaped catalyst having the physical properties as indicated in Table I (Ex-1) was tested for dehydration performance in a microflow unit consisting of a 13 mm diameter plugflow reactor, 1-phenylethanol feed vaporization facilities and product vapour condensing facilities. As 1-phenylethanol feedstock was used a sample of the process stream to the styrene reactor system of a commercial Propylene Oxide/Styrene Monomer plant. The feedstock contained 81.2% of 1-phenylethanol, 10.6% of methylphenylketone and 2% of water. The remainder up to 100% consisted of impurities and (by) products of the preceding oxidation and epoxidation sections. The outlet stream of the micro flow unit was liquefied by condensation and the resulting two-phase liquid system was analyzed by means of gas chromatographic analysis.
The dehydration experiment was carried out at test conditions of 1.0 bara pressure and a temperature of 300 °C. The feed rate of 1-phenylethanol was maintained at 30 grams per hour and the reactor tube was loaded with 20 cm3 of catalyst. The reaction was continued for approximately 140 hours after which the experiment was stopped.
Activity (conversion) and reaction selectivity of the catalyst after 50 run hours were determined from the gas chromatographic analyses of reaction product samples. Activity after 120 hours was also measured. Data are reported in Table 1. Activity and selectivity have been defined above. Example 2
The procedure as described in Example 1 was repeated, except that a different sample of feedstock containing 81.3% of 1-phenylethanol and 9.9% of methylphenylketone was used. Data are reported in Table 1 (Ex-2) . Comparison Example 1
The procedure as described in Example 1 was repeated, except that the trilobe-shaped catalyst had a BET surface area of 149 m^. Physical properties are indicated in Table 1 (Comp-Ex-1) . Only 1-phenylethanol conversion was monitored during the experiment, which was terminated after 98 hours, when 1-phenylethanol conversion was only
79%.
Comparison Example 2
The procedure as described in Example 1 was repeated, except that a star-shaped catalyst with physical properties within the ranges as described in the process according to WO 99/58480 was used. The reaction was continued for approximately 120 hours. Activity and selectivity data are given in Table 1 (Comp-Ex-2) . Comparison Example 3
The procedure as described in Example 1 was repeated, except that a trilobe-shaped catalyst with physical properties within the ranges as described in the process according to WO 99/58480 was used. A sample of feedstock containing 79.0% of 1-phenylethanol and 10.0% of methylphenylketone was used. Data are reported in Table 1 (Comp-Ex-3) . The experiment was terminated after 113 hours, when 1-phenylethanol conversion was only 91%. Activity and selectivity data are given in Table 1 (Comp-Ex-3) .
Figure imgf000010_0001
(a) Not determined
(b) Experiment stopped after 98 hours when conversion was 79%
(c) Experiment stopped after 113 hours when conversion was 91%

Claims

C L A I M S
1. A process for the preparation of styrene comprising the gas phase dehydration of 1-phenylethanol at elevated temperature in the presence of a dehydration catalyst, in which the dehydration catalyst comprises shaped alumina catalyst particles having a surface area (BET) of from 80 to 140 m2/g and a pore volume (Hg) of more than
0.65 ml/g.
2. The process according to claim 1 wherein the catalyst has a pore volume (Hg) of from 0.75 to 0.85 ml/g.
3. The process according to claim 1 and/or 2 wherein the alumina catalyst is prepared from pseudo-boehmite.
PCT/EP2004/050191 2003-02-25 2004-02-24 Process for the preparation of styrene WO2004076389A1 (en)

Priority Applications (6)

Application Number Priority Date Filing Date Title
JP2006502045A JP2006518723A (en) 2003-02-25 2004-02-24 Method for preparing styrene
BRPI0407780-6A BRPI0407780B1 (en) 2003-02-25 2004-02-24 process for the preparation of styrene.
AU2004215663A AU2004215663B2 (en) 2003-02-25 2004-02-24 Process for the preparation of styrene
DE602004028577T DE602004028577D1 (en) 2003-02-25 2004-02-24 PROCESS FOR THE PRODUCTION OF STYRENE
AT04713902T ATE477226T1 (en) 2003-02-25 2004-02-24 METHOD FOR PRODUCING STYRENE
EP04713902A EP1597216B1 (en) 2003-02-25 2004-02-24 Process for the preparation of styrene

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EP03251123 2003-02-25
EP03251123.0 2003-02-25

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EP (1) EP1597216B1 (en)
JP (1) JP2006518723A (en)
CN (1) CN1753850A (en)
AT (1) ATE477226T1 (en)
AU (1) AU2004215663B2 (en)
BR (1) BRPI0407780B1 (en)
DE (1) DE602004028577D1 (en)
RU (1) RU2323198C2 (en)
WO (1) WO2004076389A1 (en)

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EP2231559B1 (en) * 2007-12-10 2012-05-23 Shell Internationale Research Maatschappij B.V. Process for the preparation of styrene and/or a substituted styrene
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RU2750657C1 (en) * 2020-11-17 2021-06-30 Александр Адольфович Ламберов Method for producing catalyst for methylphenyl carbinol dehydration
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EP1597216A1 (en) 2005-11-23
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AU2004215663B2 (en) 2007-01-18
DE602004028577D1 (en) 2010-09-23
RU2005129744A (en) 2006-02-10
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AU2004215663A1 (en) 2004-09-10
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CN1753850A (en) 2006-03-29
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BRPI0407780B1 (en) 2013-04-24
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