EP2125678A1 - Procede d'hydrogenation d'alkylarylcetones - Google Patents
Procede d'hydrogenation d'alkylarylcetonesInfo
- Publication number
- EP2125678A1 EP2125678A1 EP07821683A EP07821683A EP2125678A1 EP 2125678 A1 EP2125678 A1 EP 2125678A1 EP 07821683 A EP07821683 A EP 07821683A EP 07821683 A EP07821683 A EP 07821683A EP 2125678 A1 EP2125678 A1 EP 2125678A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- liquid
- acetophenone
- feed
- catalyst
- process according
- 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.)
- Withdrawn
Links
- 238000000034 method Methods 0.000 title claims abstract description 40
- 150000004983 alkyl aryl ketones Chemical class 0.000 title claims abstract description 19
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 17
- 239000007788 liquid Substances 0.000 claims abstract description 83
- 239000003054 catalyst Substances 0.000 claims abstract description 45
- 239000002245 particle Substances 0.000 claims abstract description 23
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000001257 hydrogen Substances 0.000 claims abstract description 11
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 11
- 238000009904 heterogeneous catalytic hydrogenation reaction Methods 0.000 claims abstract description 3
- KWOLFJPFCHCOCG-UHFFFAOYSA-N Acetophenone Chemical group CC(=O)C1=CC=CC=C1 KWOLFJPFCHCOCG-UHFFFAOYSA-N 0.000 claims description 70
- XPNGNIFUDRPBFJ-UHFFFAOYSA-N alpha-methylbenzylalcohol Natural products CC1=CC=CC=C1CO XPNGNIFUDRPBFJ-UHFFFAOYSA-N 0.000 claims description 20
- WAPNOHKVXSQRPX-UHFFFAOYSA-N 1-phenylethanol Chemical compound CC(O)C1=CC=CC=C1 WAPNOHKVXSQRPX-UHFFFAOYSA-N 0.000 claims description 19
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 claims description 18
- 239000011541 reaction mixture Substances 0.000 claims description 14
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 claims description 8
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 claims description 5
- QQONPFPTGQHPMA-UHFFFAOYSA-N Propene Chemical compound CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 4
- GQNOPVSQPBUJKQ-UHFFFAOYSA-N 1-hydroperoxyethylbenzene Chemical compound OOC(C)C1=CC=CC=C1 GQNOPVSQPBUJKQ-UHFFFAOYSA-N 0.000 claims description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 2
- 239000001301 oxygen Substances 0.000 claims description 2
- 229910052760 oxygen Inorganic materials 0.000 claims description 2
- 238000009736 wetting Methods 0.000 description 18
- 238000006243 chemical reaction Methods 0.000 description 17
- 239000007789 gas Substances 0.000 description 14
- 230000000052 comparative effect Effects 0.000 description 13
- 229910052751 metal Inorganic materials 0.000 description 5
- 239000002184 metal Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 4
- 239000007795 chemical reaction product Substances 0.000 description 4
- 239000011521 glass Substances 0.000 description 4
- 150000002736 metal compounds Chemical class 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 3
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 3
- -1 acetophenone Chemical class 0.000 description 3
- 229910052804 chromium Inorganic materials 0.000 description 3
- 239000011651 chromium Substances 0.000 description 3
- 229910052802 copper Inorganic materials 0.000 description 3
- 239000010949 copper Substances 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- WRMNZCZEMHIOCP-UHFFFAOYSA-N 2-phenylethanol Chemical compound OCCC1=CC=CC=C1 WRMNZCZEMHIOCP-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 230000001133 acceleration Effects 0.000 description 2
- 150000001298 alcohols Chemical class 0.000 description 2
- HUMNYLRZRPPJDN-UHFFFAOYSA-N benzaldehyde Chemical compound O=CC1=CC=CC=C1 HUMNYLRZRPPJDN-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 229910052763 palladium Inorganic materials 0.000 description 2
- DTUQWGWMVIHBKE-UHFFFAOYSA-N phenylacetaldehyde Chemical compound O=CCC1=CC=CC=C1 DTUQWGWMVIHBKE-UHFFFAOYSA-N 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- WAPNOHKVXSQRPX-SPBYTNOZSA-N 1-phenylethanol Chemical class [13CH3][13CH](O)C1=CC=CC=C1 WAPNOHKVXSQRPX-SPBYTNOZSA-N 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 1
- GXDVEXJTVGRLNW-UHFFFAOYSA-N [Cr].[Cu] Chemical compound [Cr].[Cu] GXDVEXJTVGRLNW-UHFFFAOYSA-N 0.000 description 1
- 150000001491 aromatic compounds Chemical class 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 238000011021 bench scale process Methods 0.000 description 1
- 150000001555 benzenes Chemical class 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 125000001495 ethyl group Chemical group [H]C([H])([H])C([H])([H])* 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000002638 heterogeneous catalyst Substances 0.000 description 1
- 230000002262 irrigation Effects 0.000 description 1
- 238000003973 irrigation Methods 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 125000004108 n-butyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 description 1
- 125000004123 n-propyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])* 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- QNGNSVIICDLXHT-UHFFFAOYSA-N para-ethylbenzaldehyde Natural products CCC1=CC=C(C=O)C=C1 QNGNSVIICDLXHT-UHFFFAOYSA-N 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- WVDDGKGOMKODPV-ZQBYOMGUSA-N phenyl(114C)methanol Chemical compound O[14CH2]C1=CC=CC=C1 WVDDGKGOMKODPV-ZQBYOMGUSA-N 0.000 description 1
- 229940100595 phenylacetaldehyde Drugs 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
- C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
- C07C29/143—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of ketones
- C07C29/145—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of ketones with hydrogen or hydrogen-containing gases
-
- 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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/85—Chromium, molybdenum or tungsten
- B01J23/86—Chromium
-
- 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
- B01J35/40—Catalysts, in general, characterised by their form or physical properties characterised by dimensions, e.g. grain size
-
- 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
- B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C407/00—Preparation of peroxy compounds
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C409/00—Peroxy compounds
- C07C409/02—Peroxy compounds the —O—O— group being bound between a carbon atom, not further substituted by oxygen atoms, and hydrogen, i.e. hydroperoxides
- C07C409/04—Peroxy compounds the —O—O— group being bound between a carbon atom, not further substituted by oxygen atoms, and hydrogen, i.e. hydroperoxides the carbon atom being acyclic
- C07C409/08—Compounds containing six-membered aromatic rings
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
- C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
- C07C45/33—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties
- C07C45/34—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds
- C07C45/36—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds in compounds containing six-membered aromatic rings
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D301/00—Preparation of oxiranes
- C07D301/02—Synthesis of the oxirane ring
- C07D301/03—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds
- C07D301/12—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with hydrogen peroxide or inorganic peroxides or peracids
Definitions
- the present invention relates to a process for the hydrogenation of alkylaryl ketones such as acetophenone .
- Processes for hydrogenation of alkylaryl ketones such as acetophenone to the corresponding alcohols are well known in the art. Processes generally comprise hydrogenation of acetophenone by contacting feed comprising acetophenone with hydrogen at elevated pressure and temperature in the presence of a heterogeneous catalyst. Such processes have been described in prior art such as EP-A-0714877.
- US-A-6, 046, 369 teaches hydrogenation of acetophenone to 1-phenylethanol at a liquid hold-up ratio of from 30 to 90%, preferably of from 40 to 70% in order to be able to apply relatively mild process conditions such as a temperature of from 60 to 150 0 C and a pressure of from 1 MPa to 5 MPa wherein the amount of ethylbenzene produced as by-product is controlled at sufficiently low level.
- relatively mild process conditions such as a temperature of from 60 to 150 0 C and a pressure of from 1 MPa to 5 MPa wherein the amount of ethylbenzene produced as by-product is controlled at sufficiently low level.
- the use of downflow operation is discouraged in US-A-6, 046,369 (column 4, lines 8-24).
- Comparative Example 1 of US-A-6, 046 , 369 exemplifies downflow operation at a liquid hold-up ratio of 25%. In this comparative example, the conversion of acetophenone was lower and the amount of
- WO 2004/085354 relates to hydrogenation of alkylaryl ketones, such as acetophenone, in the presence of 0.5 to 30 %wt of phenolic compounds. This document contains no information on the liquid hold-up either recommended or applied for this process. Summary of the invention
- US-A-6, 046, 369 warns against the use of low liquid hold-up, that is to say less than 30%, in the hydrogenation of acetophenone .
- low liquid hold-up that is to say less than 30%
- a low liquid hold-up has the advantage that it reduces the pressure drop over a reactor.
- the present invention relates to a process for the hydrogenation of an alkylaryl ketone which process comprises contacting a feed containing an alkylaryl ketone with hydrogen in trickle-flow mode in the presence of a heterogeneous hydrogenation catalyst, in which process the dynamic liquid hold-up is of from 10 to less than 30% and the external area of the catalyst particles is effectively wetted by the liquid flowing down.
- a heterogeneous hydrogenation catalyst in which process the dynamic liquid hold-up is of from 10 to less than 30% and the external area of the catalyst particles is effectively wetted by the liquid flowing down.
- Hydrogenation within the context of the present application is understood as the chemical reaction of the alkylaryl ketones with molecular hydrogen in the presence of a suitable catalyst, as for instance described in Ullmann's Encyclopedia of Industrial Chemistry,
- alkylaryl alcohol describes ⁇ - and/or ⁇ -aryl alkanol, and mixtures thereof .
- trickle-flow mode means that liquid phase flows downward through a fixed bed of catalyst particles .
- Gas phase may flow either upward or downward.
- the liquid and gas flow velocities are so low that the liquid flows as a continuous film over the catalyst.
- the gas phase is the continuous phase in the catalyst bed.
- Criteria for obtaining trickle flow by choosing superficial velocities of gas and liquid of particular density, viscosity and surface tension, are for example given in Ullmann's Encyclopedia of Industrial Chemistry, 5th edition, Volume B4, pages 311-312.
- the process of the present invention is carried out such that the liquid is in downflow. Liquid downflow operation is advantageous in that such operation gives lower axial dispersion of the reactants, less flow non- idealities such as channelling in the catalyst bed and lower pressure drop.
- the liquid hold-up is the liquid volume contained in a unit bed volume, or the liquid volume fraction in the total bed volume.
- the dynamic liquid hold-up in a trickle-bed process concerns the liquid which drains out of the bed after the gas and liquid flows have been stopped.
- the dynamic liquid is contrary to the static liquid. Static liquid remains around the catalyst contacting points due to capillary forces.
- the dynamic liquid hold-up can be measured by a sudden shut-down of the liquid and gas feeds and closing of the gas/liquid outlet from the bottom of the reactor.
- the dynamic liquid hold-up then concerns the liquid which has drained out of the bed and collects at the bottom of the reactor.
- the dynamic liquid hold-up in the present invention is of from 10 to less than 30%, more specifically of from 10 to less than 25%, even more specifically from 15 to less than 25%, and most specifically of from 15 to 20%.
- the fraction of the external area of the catalyst particles effectively wetted by the liquid flowing down, is called the wetting efficiency.
- This wetting efficiency may, in theory, vary from 0 (0% wetting) to 1 (100% wetting) . If the liquid flows too slowly the liquid film can break up into rivulets leading to incomplete liquid coverage of the external catalyst surface. Proper design of the gas and liquid distribution and of the catalyst bed, can reduce or prevent dry zones. Typically, the wetting efficiency varies between 0.6 and 1. According to the present invention, the external area of the catalyst particles should be effectively wetted by the liquid flowing down.
- the wetting efficiency is of from 0.8 to 1.0, more specifically of from 0.9 to 1.0. More preferably, the external area of the catalyst particles is essentially completely wetted, which in this specification means that the wetting efficiency is 0.99 or higher. Most preferably, the wetting efficiency is 1.0.
- W is dimensionless and is defined as:
- W ( ⁇ * u ) / (p * d p 2 * g)
- ⁇ is the dynamic viscosity of the liquid (unit: N s ⁇ T 2 or kg s "1 ⁇ T 1 )
- u is the superficial velocity of the liquid (unit: m s "1 ), which is the quotient of the volumetric flow rate of the liquid (unit: m 3 s "1 ) divided by the cross- sectional flow area (unit: m 2 ) .
- the velocity calculated as if the reactor were empty (i.e. without any catalyst particles) is the "superficial" velocity.
- p is the specific gravity (density) of the liquid (unit : kg ⁇ T 3 ) .
- d p is the catalyst particle diameter (unit: m) .
- g is the acceleration due to gravity (which amounts to 9.81 m s ⁇ 2 ) .
- the quotient of the dynamic viscosity divided by the density of the liquid is the kinematic viscosity of the liquid (i.e. V; unit: m 2 s "1 ) .
- the above criterion as defined by Sie is also indicative for good reaction results in terms of conversion and yield, in the hydrogenation of alkylaryl ketones as is demonstrated in the Examples below with reference to the conversion of acetophenone to 1-phenylethanol . Therefore, most specifically for the present invention the above criterion as defined by Sie is satisfied. Said criterion may be satisfied by recycling part of the liquid reaction mixture to the inlet of the reactor, thereby increasing the volumetric flow rate of the liquid reaction mixture flowing through the reactor. This will increase the superficial velocity of the liquid reaction mixture, and as a consequence the wetting number W is also increased. Alternative or additional measures to achieve this, is to increase the fresh liquid feed rate and to reduce the reactor diameter, as this would also increase the superficial velocity of the liquid reaction mixture.
- Suitable catalysts for use in the present invention may contain as metal or metal compound at least one metal selected from the group consisting of groups IA, HB, VI and VIII of the Periodic System. Suitable catalysts comprise at least one of the metals or metal compounds selected from groups VI, VIII and IB, such as chromium, copper, zinc, nickel, palladium and platinum.
- the hydrogenation catalyst comprises copper, chromium and/or palladium as metal or metal compound, as these catalysts usually are not apt to hydrogenate the aromatic ring system under the conditions typically used for this process.
- the hydrogenation catalyst comprises both copper and chromium as metal or metal compound. Such catalysts have shown a high catalytic activity and selectivity over a long period of operation.
- the catalyst is activated by reduction of the catalyst before start of operation.
- the reduction of the catalyst is preferably carried out in the presence of a liquid phase with the help of hydrogen.
- a specific preferred process has been described in GB-B-587, 181.
- the alkylaryl ketones employed are ketones of alkylated benzenes in which the alkyl substituents are straight or branched alkyl substituents comprising from 2 to 10 carbon atoms, for example ethyl, n-propyl, n-butyl and/or sec-butyl substituents.
- the alkylaryl ketone to be hydrogenated in the present process is acetophenone .
- a commonly known process in which feeds containing acetophenone are produced is the preparation of propylene oxide, more specifically a process comprising: (i) contacting a feed comprising ethylbenzene with oxygen to obtain a feed comprising ethylbenzene hydroperoxide and acetophenone,
- step (ii) contacting the feed obtained in step (i) with propene in the presence of a catalyst to obtain a reaction mixture comprising propylene oxide, 1-phenylethanol and acetophenone, and
- step (iii) removing at least part of the propylene oxide and 1-phenylethanol from the reaction mixture obtained in step (ii) to obtain the feed containing acetophenone.
- the product obtained in step (ii) comprises 1- phenylethanol .
- This 1-phenylethanol can be dehydrated to obtain styrene. Therefore, the above process may further comprise (iv) dehydrating at least part of the 1-phenylethanol obtained in step (ii) to obtain styrene.
- the 1-phenylethanol can be dehydrated either when still being part of the reaction mixture as obtained in step (ii) or the 1-phenylethanol can have been separated off optionally in combination with other compounds .
- Process conditions which can be used in the process of the present invention comprise a temperature of from 50 to 250 0 C, more preferably of from 60 to 170 0 C, even more preferably of from 70 to 160 0 C, and most preferably of from 80 to 150 0 C, and a pressure of from 0.1 to
- the process according to the present invention is further illustrated by the following examples wherein a feed comprising acetophenone is hydrogenated.
- the conversion of acetophenone is expressed as the molar flow of acetophenone converted divided by the molar flow of acetophenone supplied times 100%.
- the yield of 1-phenylethanol is expressed as the molar flow of 1-phenylethanol produced divided by the molar flow of acetophenone supplied times 100%.
- the following experiment was carried out in downflow in a bench scale unit comprising a reactor connected to a heating/cooling system, a high pressure feed pump, a high pressure pump for recycling product to the feed, and two vessels (for incoming and outgoing feed streams), and a gas inlet connected to sources of hydrogen and nitrogen.
- 560 g of a copper-chromium catalyst (3 mm * 3 mm tablets) were added to the reactor.
- the bed inside the reactor comprised said catalyst particles and glass balls, which were added to fill the remaining empty space above the catalyst particles.
- the glass balls had a diameter of 3 mm and were used to provide adequate fluid distribution.
- the volume ratio of catalyst particles to glass balls was about 95:5.
- the section of the reactor containing the catalyst particles and glass balls had a cylindrical shape.
- the diameter of this cylindrical section was 32 mm.
- the reactor was first purged with nitrogen at a pressure of 2.3 * 10 ⁇ N/m 2 , then the reactor temperature was raised to 130 0 C. Hydrogen was introduced at a concentration of 1% volume, then the hydrogen concentration was gradually increased to 100% volume at a rate such that the reactor temperature did not exceed 170 0 C. The temperature was then raised to 175 0 C which temperature was maintained for 4 hours. A fresh liquid feed comprising acetophenone was then fed to the reactor at a rate of 400 g/hour, together with a hydrogen gas stream which was fed at a rate of 60 liter/hour (normal conditions). The reactor temperature was decreased by controlling the inlet temperature of the feed at 102 0 C. The outlet temperature was 113 0 C. The hydrogen pressure in the reactor was increased to
- the fresh liquid feed comprised 49.3 %wt of acetophenone, 16.5 %wt of 1-phenylethanol, 15.3 %wt of 2-phenylethanol, 8.4 %wt of ethylbenzene, 2.4 %wt of phenylacetaldehyde, 0.7 %wt of styrene, 0.4 %wt of benzylalcohol, 0.1 %wt of benzaldehyde, the remainder comprising other aromatic compounds (but no phenol in an amount of 0.1 %wt or higher) .
- Part of the liquid reaction product was recycled to the inlet of the reactor at a rate of 400 g/hour.
- the total rate of liquid feed to the inlet of the reactor was 800 g/hour, that is 1.43 g liquid/g catalyst/hours.
- the process was carried out in trickle- flow downflow mode, meaning that both liquid phase and gas phase flowed concurrently downward through the catalyst bed.
- samples were taken from the reaction product.
- the conversion of acetophenone and the yield of 1-phenylethanol were measured.
- the average conversion of acetophenone was 60.2% and the average yield of 1-phenylethanol was 55.4%.
- ethylbenzene formation from acetophenone was at an average level of 1.7 %wt on total feed.
- the dynamic liquid hold-up was measured by first shutting down the liquid and gas feeds and closing the gas/liquid outlet from the bottom of the reactor. The liquid which drained out of the bed and collected at the bottom of the reactor was measured, and amounted to 20 cm 3 . Then, after removing the drained-out liquid, the bed volume was measured by measuring the amount of ethylbenzene needed to completely fill the bed whilst the gas/liquid outlet was closed. This bed volume amounted to 151 cm 3 , and it does not include the volume occupied by the catalyst particles. The dynamic liquid hold-up could finally be calculated, and amounted to 13%.
- the wetting number W was 2 * 10 ⁇ 6 .
- W was calculated using the above-mentioned formula as given by Sie .
- the dynamic viscosity ( ⁇ ) and density (p) of the liquid reaction mixture were 6.3 * 10 ⁇ 4 kg s "1 m “1 and 906 kg ⁇ T 3 , respectively.
- the kinematic viscosity (V; i.e. ⁇ /p) of the liquid reaction mixture was therefore 7.0 * 10 ⁇ 7 m 2 s "1 .
- the particle diameter (d p ) was 3 * ICT 3 m and the acceleration due to gravity (g) is 9.81 m s "2 .
- the superficial velocity (u) of the liquid reaction mixture is defined as follows: (volumetric flow rate of the liquid) / (cross-sectional flow area) . Since the section of the reactor containing the bed had a cylindrical shape, the cross-sectional flow area is ⁇ r 2 , wherein r is the radius of the circular cross-section which is half the diameter which was 32 mm. Therefore, the cross-sectional flow area was
- the volumetric flow rate is the volume of liquid reaction mixture flowing through the bed per time unit. Therefore, the volumetric flow rate is the quotient of the sum of the fresh liquid feed rate (400 g/hr) and the recycle feed rate (400 g/hr) divided by the density of the liquid reaction mixture (906 kg ⁇ T 3 ) . Therefore, in this Comparative Example, said superficial velocity was 3.1 * 10 ⁇ 4 m s "1 .
- Example 1 Comparative Example 1 was repeated except that the inlet temperature of the feed was controlled at 90 0 C and the outlet temperature was 109 0 C. Further, part of the liquid reaction product was recycled to the inlet of the reactor at a rate of 1600 g/hour instead of 400 g/hour . Therefore, the total rate of liquid feed to the inlet of the reactor was 2000 g/hour, that is to say 2.5 times higher than in Comparative Example 1, that is 3.57 g liquid/g catalyst/hour.
- the dynamic liquid hold-up was measured in the same way as in Comparative Example 1 and amounted to 19% (29 cm 3 of liquid drained out of the bed; and a bed volume of 151 cm 3 ) .
- Example 1 the recycle feed rate was 1600 g/hr (not 400 g/hr as in Comparative Example 1) . This resulted in a different superficial velocity for Example 1, which was 7.7 * 10 ⁇ 4 m s "1 .
- Example 1 where the above-mentioned criterion for wetting efficiency (W > 4 * 10 ⁇ 6 ) was satisfied, the acetophenone conversion and the 1-phenylethanol yield were higher than in Comparative Example 1, despite the lower average reaction temperature in Example 1.
- Example 1 if the reaction temperature in Example 1 would be the same as that in Comparative Example 1, even better results would be expected for Example 1.
- Example 1 ethylbenzene formation from acetophenone was at a lower level than in Comparative Example 1.
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Abstract
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EP07821683A EP2125678A1 (fr) | 2006-10-24 | 2007-10-23 | Procede d'hydrogenation d'alkylarylcetones |
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