USRE41341E1 - Ester synthesis - Google Patents

Ester synthesis Download PDF

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USRE41341E1
USRE41341E1 US11/712,545 US71254507A USRE41341E US RE41341 E1 USRE41341 E1 US RE41341E1 US 71254507 A US71254507 A US 71254507A US RE41341 E USRE41341 E US RE41341E
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process according
range
olefin
water
ether
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US11/712,545
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Martin P. Atkins
Bhushan Sharma
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Ineos Oxide Ltd
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Ineos Europe Ltd
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Priority claimed from GBGB9515813.5A external-priority patent/GB9515813D0/en
Priority claimed from GBGB9603770.0A external-priority patent/GB9603770D0/en
Priority claimed from GBGB9613227.9A external-priority patent/GB9613227D0/en
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C67/00—Preparation of carboxylic acid esters
    • C07C67/04—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides onto unsaturated carbon-to-carbon bonds
    • 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
    • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B01J21/08—Silica
    • 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
    • B01J21/16—Clays or other mineral silicates
    • 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
    • B01J35/633—Pore volume less than 0.5 ml/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

Definitions

  • the present invention relates to a process for the synthesis of esters by reacting an olefin with a lower carboxylic acid in the presence of an acidic catalyst.
  • esters can be reacted with lower aliphatic carboxylic acids to form the corresponding esters.
  • One such method is described in GB-A-1259390 in which an ethylenically unsaturated compound is contacted with a liquid medium comprising a carboxylic acid and a free heteropolyacid of molybdenum or tungsten. This process is a homogeneous process to which the heteropolyacid catalyst is unsupported.
  • a further process for producing esters is described in JP-A-05294894 in which a lower fatty acid is esterified with a lower olefin to form a lower fatty acid ester.
  • the esterification reaction is carried out in the gaseous phase in the presence of a catalyst consisting of at least one heteropolyacid salt of a metal e.g. Li, Cu, Mg or K, being supported on a carrier.
  • a catalyst consisting of at least one heteropolyacid salt of a metal e.g. Li, Cu, Mg or K, being supported on a carrier.
  • the heteropolyacid used is phosphotungstic acid and the carrier described is silica.
  • the present invention is a process for the production of lower aliphatic esters said process comprising reacting a lower olefin with a saturated lower aliphatic mono-carboxylic acid in the vapour phase in the presence of a heteropolyacid catalyst characterised in that an amount of water in the range from 1-10 mole % based on the total of the olefin, aliphatic mono-carboxylic acid and water is added to the reaction mixture during the reaction.
  • a feature of the invention is the addition of water as a component of the reaction mixture.
  • water as a component of the reaction mixture.
  • the presence of water in the reaction mixture in an amount of 1-10 mole %, preferably from 1 to 7 mole %, e.g. 1 to 5 mole %, based on the total feed enhances the stability of the catalyst and thereby enhances the efficiency of the process.
  • the presence of water also reduces the selectivity of the process to undesired by-products such as e.g. oligomers and other unknowns, excluding diethyl ether and ethanol.
  • the amount of di-ether co-fed is suitably in the range from 1 to 6 mole %, preferably in the range from 1 to 3 mole % based on the total reaction mixture comprising the olefin, the aliphatic carboxylic acid, water and diethyl ether.
  • the di-ether co-fed may correspond to the by product di-ether from the reaction generated from the reactant olefin. Where a mixture of olefins is used, e.g. a mixture of ethylene and propylene, the di-ether may in turn be an unsymmetrical di-ether.
  • the di-ether co-feed may thus be the by-product of the reaction which by-product is recycled to the reaction mixture.
  • heteropolyacids as used herein and throughout the specification is meant to include the free acids.
  • the heteropolyacids used to prepare the esterification catalysts of the present invention therefore include inter alia the free acids and coordination type salts thereof in which the anion is a complex, high molecular weight entity.
  • the anion is comprises 2-18 oxygen-linked polyvalent metal atoms, which are called peripheral atoms. These peripheral atoms surround one or more central atoms in a symmetrical manner.
  • the peripheral atoms are usually one or more of molybdenum, tungsten, vanadium, niobium, tantalum and other metals.
  • the central atoms are usually silicon or phosphorus but can comprise any one of a large variety of atoms from Groups I-VIII in the Periodic Table of elements. These include, for instance, cupric ions; divalent beryllium, zinc, cobalt or nickel ions; trivalent boron, aluminium, gallium, iron, cerium, arsenic, antimony, phosphorus, bismuth, chromium or rhodium ions; tetravalent silicon, germanium, tin, titanium, zirconium, vanadium, sulphur, tellurium, manganese nickel, platinum, thorium, hafnium, cerium ions and other rare earth ions; pentavalent phosphorus, arsenic, vanadium, antimony ions; hexavalent tellurium ions; and heptavalent iodine ions.
  • heteropolyacids are also known as “polyoxoanions”, “polyoxometallates” or “metal oxide clusters”.
  • polyoxoanions polyoxometallates
  • metal oxide clusters metal oxide clusters.
  • Heteropolyacids usually have a high molecular weight e.g. in the range from 700-8500 and include dimeric complexes. They have a relatively high solubility in polar solvents such as water or other oxygenated solvents, especially if they are free acids and in the case of several salts, and their solubility can be controlled by choosing the appropriate counter-ions.
  • polar solvents such as water or other oxygenated solvents
  • heteropolyacids that may be used as the catalysts in the present invention include:
  • the heteropolyacid catalyst whether used as a free acid or as a salt thereof is suitably supported, preferably on a siliceous support.
  • the siliceous support is suitably in the form of extrudates or pellets.
  • the siliceous support used is most preferably derived from an amorphous, non-porous synthetic silica especially fumed silica, such as those produced by flame hydrolysis of SiCl 4 .
  • Specific examples of such siliceous supports include Support 350 made by pelletisation of AEROSIL® 200 (both ex Degussa). This pelletisation procedure is suitably carried out by the process described in U.S. Pat. No. 5,086,031 (see especially the Examples) and is incorporated herein by reference. Such a process of pelletisation or extrusion does not involve any steam treatment steps and the porosity of the support is derived from the interstices formed during the pelletisation or extrusion step of the non-porous silica.
  • the silica support is suitably in the form of pellets or beads or are globular in shape having an average particle diameter of 2 to 10 mm, preferably 4 to 6 mm.
  • the siliceous support suitably has a pore volume in the range from 0.3-1.2 ml/g, preferably from 0.6-1.0 ml/g.
  • the support suitably has a crush strength of at least 2 Kg force, suitably at least 5 Kg force, preferably at least 6 Kg and more preferably at least 7 Kg.
  • the crush strengths quoted are based on average of that determined for each set of 50 beads/globules on a CHATTILLON tester which measures the minimum force necessary to crush a particle between parallel plates.
  • the bulk density of the support is suitably at least 380 g/l, preferably at least 440 g/l.
  • the support suitably has an average pore radius (prior to use) of 10 to 500 ⁇ preferably an average pore radius of 30 to 100 ⁇ .
  • the siliceous support is suitably free of extraneous metals or elements which might adversely affect the catalytic activity of the system.
  • the siliceous support suitably has at least 99% w/w purity, i.e. the impurities are less than 1% w/w, preferably less than 0.60% w/w and more preferably less than 0.30% w/w.
  • pelleted silica supports are the Grace 57 and 1371 grades of silica.
  • Grace silica No. 1371 has an average bulk density of about 0.39 g/ml, an average pore volume of about 1.15 ml/g and an average particle size ranging from about 0.1-3.5 mm. These pellets can be used as such or after crushing to an average particle size in the range from 0.5-2 mm and sieving before being used as the support for the heteropolyacid catalyst.
  • the impregnated support is suitably prepared by dissolving the heteropolyacid, which is preferably a tungstosilicic acid, in e.g. distilled water, and then adding the support to the aqueous solution so formed.
  • the support is suitably let to soak in the acid solution for a duration of several hours, with periodic manual stirring, after which time it is suitably filtered using a Buchner funnel in order to remove any excess acid.
  • the wet catalyst thus formed is then suitably placed in an oven at elevated temperature for several hours to dry, after which time it is allowed to cool to ambient temperature in a desiccator.
  • the weight of the catalyst on drying, the weight of the support used and the weight of the acid on support was obtained by deducting the latter from the former from which the catalyst loading in g/liter was determined.
  • the support may be impregnated with the catalyst using the incipient wetness technique with simultaneous drying on a rotary evaporator.
  • This supported catalyst (measured by weight) can then be used in the esterification process.
  • the amount of heteropolyacid deposited/impregnated on the support for use in the esterification reaction is suitably in the range from 10 to 60% by weight, preferably from 30 to 50% by weight based on the total weight of the heteropolyacid and the support.
  • the olefin reactant used is suitably ethylene, propylene or mixtures thereof Where a mixture of olefins is used, the resultant product will inevitably a mixture of esters.
  • the source of the olefin reactant used may be a refinery product or a chemical grade olefin which invariably contain some alkanes admixed therewith.
  • the saturated, lower aliphatic mono-carboxylic acid reactant is suitably a C1-C4 carboxylic acid and is preferably acetic acid.
  • the reaction mixture suitably comprises a molar excess of the olefin reactant with respect to the aliphatic monocarboxylic acid reactant.
  • the mole ratio of olefin to the lower carboxylic acid in the reaction mixture is suitably in the range from 1:1 to 15:1, preferably from 10:1 to 14:1.
  • the reaction is carried out in the vapour phase suitably above the dew point of the reactor contents comprising the reactant acid, any alcohol formed in situ, the product ester and water as stated above.
  • the amount of water is in the range from 1-10 mole %, suitably from 1-7 mole %, preferably from 1-5 mole % based on the total amount of olefin, carboxylic acid and water.
  • Dew point is the temperature at which condensation of a vapour of a given sample in air takes place. The dew point of any vaporous sample will depend upon its composition.
  • the supported heteropolyacid catalyst is suitably used as a fixed bed which may be in the form of a packed column.
  • the vapours of the reactant olefins and acids are passed over the catalyst suitably at a GHSV in the range from 100 to 5000 per hour, preferably from 300 to 2000 per hour.
  • the esterification reaction is suitably carried out at a temperature in the range from 150°-200° C. using a reaction pressure which is at least 400 KPa, preferably from 500-3000 Kpa depending upon the relative mole ratios of olefin to acid reactant and the amount of water used.
  • the water added to the reaction mixture is suitably present in the form of steam and is capable of generating a mixture of esters and alcohols in the process.
  • the products of the reaction are recovered by e.g. fractional distillation.
  • esters are produced, whether singly or as mixture of esters, these may be hydrolysed to the corresponding alcohols or mixture of alcohols in relatively high yields and purity.
  • Silica granules (Grace 1371 grade, 530 m 2 /g, bulk density 0.39 g/ml, pore volume 1.15 ml/g, ca. 1-3 mm, 70 g, ex W R Grace) were soaked over 24 hours with intermittent stirring in a solution of silicotungstic acid [H 4 SiW 12 O 40 .26H 2 O] (65.53 g, ex Japan New Metals) dissolved in 250 mlo distilled water in order to impregnate the silica support with the silicophosphoric acid catalyst. After this duration, excess catalyst solution was decanted and filtered off. The resultant catalyst impregnated support was then dried in flowing nitrogen gas overnight at 120° C. The supported catalyst so formed was then left in a desiccator to cool and was finally reweighed. The resultant support catalyst had a heteropolyacid catalyst loading of 92 g/liter.
  • Catalyst 2 Silica granules (Grace 57 grade, surface area 510 m 2 /g, bulk density 0.649 g/ml, pore volume 1.0267 ml/g, ca. 5-8 mm, 57.7 g, ex W R Grace) was soaked in a solution of 12-tungstosilicic acid [H 4 SiW 12 O 40 .26H 2 O] (ex Johnson Matthey, 69.4 dissolved in 200 ml distilled water) for 24 hours with intermittent stirring in order to impregnate the support with the catalyst. Thereafter the excess solution of the silicotungstic acid catalyst was removed by decantation and filtration. The resultant catalyst impregnated support was then dried overnight under flowing nitrogen at 120° C. The dried supported catalyst so formed was cooled in a desiccator and had a heteropolyacid catalyst loading of 190g/liter.
  • Catalyst 3 The above process of Catalyst 2 was repeated and was found to have a heteropolyacid catalyst loading of 192 g/liter.
  • the reactor used was a three-zone Severn Sciences reactor constructed of Hastelloy C-276 capable of withstanding glacial acetic acid up to 300° C. and 15000 Kpa (150 barg) pressure (length 650 mm, outer diameter 22 mm, internal diameter 16 mm). It had a thermowell running the entire reactor length (5 mm outer diameter) and 1.77 cm outer diameter Swagelock VCR joints at each end. Gas from cylinders of ethylene and nitrogen were taken off at 1000 Kpa (10 barg) and then compressed to 5000-12000 Kpa (50-120 barg), via Haskel boosters, before being regulated and fed to mass-flow controllers. The liquid feed systems had 2 dm 3 reservoirs maintained under a nitrogen blanket of 10 KPa-80 KPa (0.1-0.8 barg).
  • a cooling jacket was provided to condense products in the gas stream back to liquids prior to collection in a receiver. The majority of the liquid product was collected at room temperature.
  • a pre-heating zone was located upstream of the catalyst bed.
  • the pre-heating zone was separated from the catalyst bed by a plug of glass wool.
  • Another plug of gas wool was used downstream of the catalyst bed to reduce dead volume and help maintain the catalyst bed in the centre section of the reactor.
  • the reaction was started up by pressurising the reactor to 1000 KPa (10 barg) with nitrogen, establishing the desired flow rate (which is the same as that used later for the olefin feed) and then increasing the reactor temperature to the desired operating conditions (170° C. or 180° C.) over a one hour period.
  • the liquid pump for the mixture of acetic acid/water mixture was switched on initially at the desired flow rate and the olefin admitted into the reactor on liquid breakthrough at the collection pots, usually after 2 to 3 hours.
  • the flows were then adjusted to give the desired feed molar ratios and GHSVs.
  • the reactor effluent was collected at regular intervals. Liquid product was drained off, weighed and then analysed by GC.
  • the gas stream was sampled downstream of the liquid collection points and also analysed by GC. Total gas out during a test period was measured using a wet-gas meter.
  • Catalyst 1 Catalyst 2 Catalyst 3 Volume (cm 3 ) 25 25 25 25 Weight (g) 11.3 (11.4*) 12 12 Pellet size (mm) 1-2 (0.5-1*) 0.5-1 0.5-1 Bed length 8.75 (14*) 14 14 *Parameters of Catalyst 1 used for the Runs in Table 2
  • Solution “A” was added to pelleted silica support (Grace 1371 grade, 1-3 mm, 99.5 g, ex W R Grace) and left to soak over 24 hours with occasional stirring in order to impregnate the silica with the tungstophosphoric acid catalyst. After this duration, excess solution “A” was decanted and filtered off. The resultant catalyst impregnated support was then dried in flowing nitrogen gas initially at 150° C. for 3 hours and then raised to 200° C. and maintained at that temperature for 5 hours. The supported catalyst so formed was then left in a desiccator to cool and was finally reweighed.
  • the resultant supported catalyst had a final weight of 164.4 g, a net catalyst loading of 64.9 g and had the formula Li 0.1 H 2.9 PW 12 O 40 .24H 2 O/SiO 2 corresponding to a loading of 255 g/l.
  • Catalyst 4 Pelleted silica support (Grace 1371 grade, 1-3 mm, 70 g, ex W R Grace) was soaked in a solution (250 ml) of 12-tungstosilicic acid [H 4 SiW 12 O 40 .26H 2 O] (65.53 g in distilled water) for 24 hours with intermittent stirring in order to impregnate the support with the catalyst. Thereafter the excess solution of the tungstosilicic acid was removed by decantation and filtration. The resultant catalyst impregnated support was then dried overnight under flowing nitrogen at 120° C.
  • the dried supported catalyst so formed was cooled in a desiccator and had a final weight of 86.2 g, a net catalyst loading of 16.2 g and had the formula H 4 SiW 12 O 40 .26H 2 O/SiO 2 corresponding to a loading of 92 g/l.
  • Catalyst 4 Catalyst 5 Volume (cm 3 ) 25 25 Weight (g) 15.5 11.2-11.4 Pellet size (mm) 1-2 1-2 (Table 11) & 0.5-1 (Tables 12, 13 and 14) Bed length 8.5 8.75
  • Run No. 28 Run No. 29 Run No. 30 (Catalyst 5-11.3 g) Run Conditions: Parameters HOS 1-2 17-20 21-24 Temperature (° C.) Applied 170 170 170 Bed (T/M/B) 176/—/174 173/—/170 173/—/170 Pressure (Kpa) 1000 1000 1000 Total feed GHSV/h (@ STP) 980 980 980 C 2 H 4 GHSV/h 905 905 905 HAC GHSV/h 66 66 66 H 2 O GHSV/h 9 9 9 C 2 H 4 (g/Lcat/h) 1131 1131 1131 HAC (g/Lcat/h) 177 177 177 H 2 O (g/Lcat/h) 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8 8

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Abstract

This invention relates to a process for the production of lower aliphatic esters by reacting a lower olefin with a saturated lower aliphatic mono-carboxylic acid in the vapor phase in the presence of a heteropolyacid catalyst characterized in that an amount of water in the range from 1-10 mole % based on the total of the olefin, aliphatic monocarboxylic acid and water is added to the reaction mixture during the reaction. The presence of water enhances the yield of the desired ester. The reaction mixture may optionally contain a di-ether to minimize the by-products.
The process is particularly suitable for producing ethyl acetate from ethylene and acetic acid in the presence of water.

Description

The present invention relates to a process for the synthesis of esters by reacting an olefin with a lower carboxylic acid in the presence of an acidic catalyst.
It is well known that olefins can be reacted with lower aliphatic carboxylic acids to form the corresponding esters. One such method is described in GB-A-1259390 in which an ethylenically unsaturated compound is contacted with a liquid medium comprising a carboxylic acid and a free heteropolyacid of molybdenum or tungsten. This process is a homogeneous process to which the heteropolyacid catalyst is unsupported. A further process for producing esters is described in JP-A-05294894 in which a lower fatty acid is esterified with a lower olefin to form a lower fatty acid ester. In this document, the esterification reaction is carried out in the gaseous phase in the presence of a catalyst consisting of at least one heteropolyacid salt of a metal e.g. Li, Cu, Mg or K, being supported on a carrier. The heteropolyacid used is phosphotungstic acid and the carrier described is silica.
It has now been found that the process efficiency can be improved significantly by co-feeding water to the reaction mixture.
Accordingly, the present invention is a process for the production of lower aliphatic esters said process comprising reacting a lower olefin with a saturated lower aliphatic mono-carboxylic acid in the vapour phase in the presence of a heteropolyacid catalyst characterised in that an amount of water in the range from 1-10 mole % based on the total of the olefin, aliphatic mono-carboxylic acid and water is added to the reaction mixture during the reaction.
A feature of the invention is the addition of water as a component of the reaction mixture. Surprisingly, it has been fond that the presence of water in the reaction mixture in an amount of 1-10 mole %, preferably from 1 to 7 mole %, e.g. 1 to 5 mole %, based on the total feed enhances the stability of the catalyst and thereby enhances the efficiency of the process. Furthermore, the presence of water also reduces the selectivity of the process to undesired by-products such as e.g. oligomers and other unknowns, excluding diethyl ether and ethanol.
It has further been found that dosing the reaction mixture with amounts of di-ether such as e.g. diethyl ether, as a co-feed also reduces the formation of undesirable by-products. The amount of di-ether co-fed is suitably in the range from 1 to 6 mole %, preferably in the range from 1 to 3 mole % based on the total reaction mixture comprising the olefin, the aliphatic carboxylic acid, water and diethyl ether. The di-ether co-fed may correspond to the by product di-ether from the reaction generated from the reactant olefin. Where a mixture of olefins is used, e.g. a mixture of ethylene and propylene, the di-ether may in turn be an unsymmetrical di-ether. The di-ether co-feed may thus be the by-product of the reaction which by-product is recycled to the reaction mixture.
The term “heteropolyacids” as used herein and throughout the specification is meant to include the free acids. The heteropolyacids used to prepare the esterification catalysts of the present invention therefore include inter alia the free acids and coordination type salts thereof in which the anion is a complex, high molecular weight entity. Typically, the anion is comprises 2-18 oxygen-linked polyvalent metal atoms, which are called peripheral atoms. These peripheral atoms surround one or more central atoms in a symmetrical manner. The peripheral atoms are usually one or more of molybdenum, tungsten, vanadium, niobium, tantalum and other metals. The central atoms are usually silicon or phosphorus but can comprise any one of a large variety of atoms from Groups I-VIII in the Periodic Table of elements. These include, for instance, cupric ions; divalent beryllium, zinc, cobalt or nickel ions; trivalent boron, aluminium, gallium, iron, cerium, arsenic, antimony, phosphorus, bismuth, chromium or rhodium ions; tetravalent silicon, germanium, tin, titanium, zirconium, vanadium, sulphur, tellurium, manganese nickel, platinum, thorium, hafnium, cerium ions and other rare earth ions; pentavalent phosphorus, arsenic, vanadium, antimony ions; hexavalent tellurium ions; and heptavalent iodine ions. Such heteropolyacids are also known as “polyoxoanions”, “polyoxometallates” or “metal oxide clusters”. The structures of some of the well known anions are named after the original researchers in this field and are known e.g. as Keggin, Wells-Dawson and Anderson-Evans-Perloff structures.
Heteropolyacids usually have a high molecular weight e.g. in the range from 700-8500 and include dimeric complexes. They have a relatively high solubility in polar solvents such as water or other oxygenated solvents, especially if they are free acids and in the case of several salts, and their solubility can be controlled by choosing the appropriate counter-ions. Specific examples of heteropolyacids that may be used as the catalysts in the present invention include:
    • 12-tungstophosphoric acid—H3[PW12O40].xH2O
    • 12-molybdophosphoric acid—H3[PMo12O40].xH2O
    • 12-tungstosilicic acid—H4[SiW12O40].xH2O
    • 12-molybdosilicic acid—H4[SiMo12O40].xH2O
    • Potassium tungstophosphate—K6[P2W18O62].xH2O
    • Sodium molybdophosphate—Na3[PMo12O40].xH2O
    • Ammonium molybdodiphosphate—(NH4)6[P2Mo18O62].xH2O
    • Sodium tungstonickelate—Na4[NiW6O24H6].xH2O
    • Ammonium molybdodicobaltate—(NH4)[Co2Mo10O36].xH2O
    • Cesium hydrogen tungstosilicate—Cs3H[SiW12O40].xH2O
    • Potassium molybdodivanado phosphate—K5[PMoV2O40].xH2O
The heteropolyacid catalyst whether used as a free acid or as a salt thereof is suitably supported, preferably on a siliceous support. The siliceous support is suitably in the form of extrudates or pellets.
The siliceous support used is most preferably derived from an amorphous, non-porous synthetic silica especially fumed silica, such as those produced by flame hydrolysis of SiCl4. Specific examples of such siliceous supports include Support 350 made by pelletisation of AEROSIL® 200 (both ex Degussa). This pelletisation procedure is suitably carried out by the process described in U.S. Pat. No. 5,086,031 (see especially the Examples) and is incorporated herein by reference. Such a process of pelletisation or extrusion does not involve any steam treatment steps and the porosity of the support is derived from the interstices formed during the pelletisation or extrusion step of the non-porous silica. The silica support is suitably in the form of pellets or beads or are globular in shape having an average particle diameter of 2 to 10 mm, preferably 4 to 6 mm. The siliceous support suitably has a pore volume in the range from 0.3-1.2 ml/g, preferably from 0.6-1.0 ml/g. The support suitably has a crush strength of at least 2 Kg force, suitably at least 5 Kg force, preferably at least 6 Kg and more preferably at least 7 Kg. The crush strengths quoted are based on average of that determined for each set of 50 beads/globules on a CHATTILLON tester which measures the minimum force necessary to crush a particle between parallel plates. The bulk density of the support is suitably at least 380 g/l, preferably at least 440 g/l.
The support suitably has an average pore radius (prior to use) of 10 to 500 Å preferably an average pore radius of 30 to 100 Å.
In order to achieve optimum performance, the siliceous support is suitably free of extraneous metals or elements which might adversely affect the catalytic activity of the system. The siliceous support suitably has at least 99% w/w purity, i.e. the impurities are less than 1% w/w, preferably less than 0.60% w/w and more preferably less than 0.30% w/w.
Other pelleted silica supports are the Grace 57 and 1371 grades of silica. In particular, Grace silica No. 1371 has an average bulk density of about 0.39 g/ml, an average pore volume of about 1.15 ml/g and an average particle size ranging from about 0.1-3.5 mm. These pellets can be used as such or after crushing to an average particle size in the range from 0.5-2 mm and sieving before being used as the support for the heteropolyacid catalyst.
The impregnated support is suitably prepared by dissolving the heteropolyacid, which is preferably a tungstosilicic acid, in e.g. distilled water, and then adding the support to the aqueous solution so formed. The support is suitably let to soak in the acid solution for a duration of several hours, with periodic manual stirring, after which time it is suitably filtered using a Buchner funnel in order to remove any excess acid.
The wet catalyst thus formed is then suitably placed in an oven at elevated temperature for several hours to dry, after which time it is allowed to cool to ambient temperature in a desiccator. The weight of the catalyst on drying, the weight of the support used and the weight of the acid on support was obtained by deducting the latter from the former from which the catalyst loading in g/liter was determined.
Alternatively, the support may be impregnated with the catalyst using the incipient wetness technique with simultaneous drying on a rotary evaporator.
This supported catalyst (measured by weight) can then be used in the esterification process. The amount of heteropolyacid deposited/impregnated on the support for use in the esterification reaction is suitably in the range from 10 to 60% by weight, preferably from 30 to 50% by weight based on the total weight of the heteropolyacid and the support.
In the esterification reaction, the olefin reactant used is suitably ethylene, propylene or mixtures thereof Where a mixture of olefins is used, the resultant product will inevitably a mixture of esters. The source of the olefin reactant used may be a refinery product or a chemical grade olefin which invariably contain some alkanes admixed therewith.
The saturated, lower aliphatic mono-carboxylic acid reactant is suitably a C1-C4 carboxylic acid and is preferably acetic acid.
The reaction mixture suitably comprises a molar excess of the olefin reactant with respect to the aliphatic monocarboxylic acid reactant. Thus the mole ratio of olefin to the lower carboxylic acid in the reaction mixture is suitably in the range from 1:1 to 15:1, preferably from 10:1 to 14:1.
The reaction is carried out in the vapour phase suitably above the dew point of the reactor contents comprising the reactant acid, any alcohol formed in situ, the product ester and water as stated above. The amount of water is in the range from 1-10 mole %, suitably from 1-7 mole %, preferably from 1-5 mole % based on the total amount of olefin, carboxylic acid and water. Dew point is the temperature at which condensation of a vapour of a given sample in air takes place. The dew point of any vaporous sample will depend upon its composition. The supported heteropolyacid catalyst is suitably used as a fixed bed which may be in the form of a packed column. The vapours of the reactant olefins and acids are passed over the catalyst suitably at a GHSV in the range from 100 to 5000 per hour, preferably from 300 to 2000 per hour.
The esterification reaction is suitably carried out at a temperature in the range from 150°-200° C. using a reaction pressure which is at least 400 KPa, preferably from 500-3000 Kpa depending upon the relative mole ratios of olefin to acid reactant and the amount of water used.
The water added to the reaction mixture is suitably present in the form of steam and is capable of generating a mixture of esters and alcohols in the process. The products of the reaction are recovered by e.g. fractional distillation. Where esters are produced, whether singly or as mixture of esters, these may be hydrolysed to the corresponding alcohols or mixture of alcohols in relatively high yields and purity. By using this latter technique the efficiency of the process to produce alcohols from olefins is significantly improved over the conventional process of producing alcohols by hydration of olefins.
The present invention is further illustrated with reference to the following Examples and Comparative Tests.
EXAMPLES
In all the Examples, the reaction conditions used and the results achieved are tabulated below. In these tables, the following abbreviations have been used:
HOS Hours on stream
Bed (T/M/B) Bed (top/middle/bottom)
HAC Acetic Acid
C2H4 Ethylene
H2O Water
EtAc Ethyl acetate
EtOH Ethanol
DEE Diethyl ether
GHSV Gas hourly space velocity
g/Lcat/h Gram per liter of catalyst per hour
STP Standard temperature & pressure
STY Space time yield
Example 1
A. Catalyst Preparations
Catalyst 1
Silica granules (Grace 1371 grade, 530 m2/g, bulk density 0.39 g/ml, pore volume 1.15 ml/g, ca. 1-3 mm, 70 g, ex W R Grace) were soaked over 24 hours with intermittent stirring in a solution of silicotungstic acid [H4SiW12O40.26H2O] (65.53 g, ex Japan New Metals) dissolved in 250 mlo distilled water in order to impregnate the silica support with the silicophosphoric acid catalyst. After this duration, excess catalyst solution was decanted and filtered off. The resultant catalyst impregnated support was then dried in flowing nitrogen gas overnight at 120° C. The supported catalyst so formed was then left in a desiccator to cool and was finally reweighed. The resultant support catalyst had a heteropolyacid catalyst loading of 92 g/liter.
Catalyst 2: Silica granules (Grace 57 grade, surface area 510 m2/g, bulk density 0.649 g/ml, pore volume 1.0267 ml/g, ca. 5-8 mm, 57.7 g, ex W R Grace) was soaked in a solution of 12-tungstosilicic acid [H4SiW12O40.26H2O] (ex Johnson Matthey, 69.4 dissolved in 200 ml distilled water) for 24 hours with intermittent stirring in order to impregnate the support with the catalyst. Thereafter the excess solution of the silicotungstic acid catalyst was removed by decantation and filtration. The resultant catalyst impregnated support was then dried overnight under flowing nitrogen at 120° C. The dried supported catalyst so formed was cooled in a desiccator and had a heteropolyacid catalyst loading of 190g/liter.
Catalyst 3: The above process of Catalyst 2 was repeated and was found to have a heteropolyacid catalyst loading of 192 g/liter.
B. Catalyst Forming
All the catalysts produced above were broken down and sieved to obtain the desired pellet size for loading into the esterification reactor.
C. Catalyst Testing
The reactor used was a three-zone Severn Sciences reactor constructed of Hastelloy C-276 capable of withstanding glacial acetic acid up to 300° C. and 15000 Kpa (150 barg) pressure (length 650 mm, outer diameter 22 mm, internal diameter 16 mm). It had a thermowell running the entire reactor length (5 mm outer diameter) and 1.77 cm outer diameter Swagelock VCR joints at each end. Gas from cylinders of ethylene and nitrogen were taken off at 1000 Kpa (10 barg) and then compressed to 5000-12000 Kpa (50-120 barg), via Haskel boosters, before being regulated and fed to mass-flow controllers. The liquid feed systems had 2 dm3 reservoirs maintained under a nitrogen blanket of 10 KPa-80 KPa (0.1-0.8 barg).
A cooling jacket was provided to condense products in the gas stream back to liquids prior to collection in a receiver. The majority of the liquid product was collected at room temperature.
A pre-heating zone was located upstream of the catalyst bed. The pre-heating zone was separated from the catalyst bed by a plug of glass wool. Another plug of gas wool was used downstream of the catalyst bed to reduce dead volume and help maintain the catalyst bed in the centre section of the reactor.
The reaction was started up by pressurising the reactor to 1000 KPa (10 barg) with nitrogen, establishing the desired flow rate (which is the same as that used later for the olefin feed) and then increasing the reactor temperature to the desired operating conditions (170° C. or 180° C.) over a one hour period. The liquid pump for the mixture of acetic acid/water mixture was switched on initially at the desired flow rate and the olefin admitted into the reactor on liquid breakthrough at the collection pots, usually after 2 to 3 hours. The flows were then adjusted to give the desired feed molar ratios and GHSVs. The reactor effluent was collected at regular intervals. Liquid product was drained off, weighed and then analysed by GC. The gas stream was sampled downstream of the liquid collection points and also analysed by GC. Total gas out during a test period was measured using a wet-gas meter.
The above process/catalysts were used to esterify ethylene with acetic acid. The relative amounts of each of the Catalysts 1 to 3 used, their bed size and bed length in performing the esterification reaction were as follows:
Parameter Catalyst 1 Catalyst 2 Catalyst 3
Volume (cm3) 25 25 25
Weight (g) 11.3 (11.4*) 12 12
Pellet size (mm) 1-2 (0.5-1*) 0.5-1 0.5-1
Bed length 8.75 (14*) 14 14
*Parameters of Catalyst 1 used for the Runs in Table 2
TABLE 1
Run Conditions: (1 Mole % Water added to feed) using Catalyst 1:
Parameters Run No. 1 Run No. 2 Run No. 3*
HOS 17-20 42-45 70-73
(21-24)
Temperature (° C.)
Applied 170 170 170
Bed (T/M/B) 173/—/170 172.5/—/169.5 173/—/168
Pressure (Kpa) 1000 1000 1000
Total feed GHSV/h 980 980 974
(@ STP)
C2H4 GHSV/h 905 905 905
HAC GHSV/h 66 66 69
H2O GHSV/h 9 9 9
C2H4 (g/Lcat/h) 1131 1131 1131
HAC (g/Lcat/h) 177 177 185
H2O (g/Lcat/h) 8 8 0
Feed contact time 4 4 4
[1/GHSV](secs)
C2H4/HAC/H2O 92.3/6.7/1.0 92.3/6.7/1.0 92.9/14.1/0
mole % ratio
C2H4/HAC/H2O wt % ratio 85.9/13.5/0.6 85.9/13.5/0.6 85.9/14.1/0
C2H4/HAC mole ratio 13.7 13.7 13.1
*No added water used in this comparative test (not according to the
invention)
Product Analysis
Products/Analysis Run No. 1 Run No. 2 Run No. 3*
HAC Conversion 66 64 27
Product Selectivity (wt %)
EtAc 97.3 97.8 91.6
EtOH 0.4 0.3 0.1
DEE 1.8 1.3 0.0
Acetaldehyde 0.0 0.0 0.0
Oligomers 0.3 0.6 1.4
Others 0.1 0.04 6.8
EtAc Yield 95 59 25
EtAc STY (g/Lcat/h) 180 160 44
Carbon Balance (mol %) 104 105 100
Oxygen Balance (mol %) 95 102 81
Mass Balance 103 105 99
Water recovered (%) 69 73 —
*No water used and is hence a comparative test (not according to the invention)
TABLE 2
Run Conditions: (1 Mole % Water added to feed) using Catalyst 1:
Parameters Run No. 4 Run No. 5 Run No. 6 Run No. 7
HOS 19-22 44-77 68.75-73.75 91-94
Temperature (° C.)
Applied 180 180 180 180
Bed (T/M/B) 181.5/186/182.5 181.5/185/183 181.3/184.5/181.2 181.4/184/181.1
Pressure (Kpa) 1000 1000 1000 1000
Total feed GHSV/h (@ STP) 980 980 980 980
C2H4 GHSV/h 905 905 905 905
HAC GHSV/h 66 66 66 66
H2O GHSV/h 9 9 9 9
C2H4 (g/Lcat/h) 1131 1131 1131 1131
HAC (g/Lcat/h) 177 177 177 177
H2O (g/Lcat/h) 8 8 8 8
Feed contact time [1/GHSV](secs) 4 4 4 4
C2H4/HAC/H2O mole % ratio 92.3/6.7/1.0 92.3/6.7/1.0 92.3/6.7/1.0 92.3/6.7/1.0
C2H4/HAC/H2O wt % ratio 86/13.4/0.6 86/13.4/0.6 86/13.4/0.6 86/13.4/0.6
C2H4/HAC mole ratio 13.7 13.7 13.7 13.7
Product Analysis
Products/Analysis Run No. 4 Run No. 5 Run No. 6 Run No. 7
Ethylene conversion (%) 5.3 3.9 4.1 6.0
HAC Conversion 71 64 60 54
Product Selectivity (wt %)
EtAc 95.9 97.2 97.8 98.1
EtOH 0.7 0.6 0.5 0.6
DEE 2.3 1.8 1.3 1.0
Acetaldehyde 0.0 0.0 0.0 0.0
Oligomers 0.8 0.3 0.6 0.2
Others 0.3 0.1 0.0 0.0
EtAc Yield 68 63 59 53
EtAc STY (g/Lcat/h) 194 183 164 148
Carbon Balance (mol %) 100 199 100 97
Oxygen Balance (mol %) 94 89 93 88
Mass Balance 100 99 99 96
Water recovered (%) 53 56 62 65
TABLE 3
Run Conditions: (1 Mole % Water added to feed) using Catalyst 2:
Parameters Run No. 8 Run No. 9 Run No. 10
HOS 14.75-17.5 38.5-41.5 62.5-65.5
Temperature (° C.)
Applied 180 180 180
Bed (T/M/B) 179.5/189/ 179.6/187.5/ 179.4/186.5/
182.8 182.9 182.8
Pressure (Kpa) 1000 1000 1000
Total feed GHSV/h (@ STP) 981 981 981
C2H4 GHSV/h 905 905 905
HAC GHSV/h 66 66 66
H2O GHSV/h 10 10 10
C2H4 (g/Lcat/h) 1131 1131 1131
HAC (g/Lcat/h) 177 177 177
H2O (g/Lcat/h) 8 8 8
Feed contact time 4 4 4
[1/GHSV](secs)
C2H4/HAC/H2O 92.3/6.7/1.0 92.3/6.7/1.0 92.9/6.7/1.0
mole % ratio
C2H4/HAC/H2O wt % ratio 85.9/13.5/0.6 85.9/13.5/0.6 85.9/13.5/0.6
C2H4/HAC mole ratio 13.7 13.7 13.7
Product Analysis
Products/Analysis Run No. 8 Run No. 9 Run No. 10
Ethylene Conversion 7.3 3.9 3.3
HAC Conversion 81 77 75
Product Selectivity (wt %)
EtAc 92.7 95.2 96.0
EtOH 0.8 0.7 0.7
DEE 3.8 2.8 2.2
Acetaldehyde 0.0 0.0 0.0
Oligomers 1.6 0.9 0.8
Others 1.1 0.5 0.3
EtAc Yield 75 73 72
EtAc STY (g/Lcat/h) 213 211 201
Carbon Balance (mol %) 100 102 103
Oxygen Balance (mol %) 99 96 98
Mass Balance 100 102 103
Water recovered (%) 45 43 51
TABLE 4
Run Conditions: (5 Mole % Water added to feed) using Catalyst 2:
Parameters Run No. 11 Run No. 12 Run No. 13
HOS 90.5-95.5 134.5-137.5 158.5-161.5
Temperature (° C.)
Applied 180 180 180
Bed (T/M/B) 179.3/188.5/ 179.6/188.5/ 179.5/188.5/
182.4 183.4 183.4
Pressure (Kpa) 1000 1000 1000
Total feed GHSV/h (@ STP) 975 975 975
C2H4 GHSV/h 866 866 866
HAC GHSV/h 61 61 61
H2O GHSV/h 48 48 48
C2H4 (g/Lcat/h) 1083 1083 1083
HAC (g/Lcat/h) 164 164 164
H2O (g/Lcat/h) 38 38 38
Feed contact time 4 4 4
[1/GHSV](secs)
C2H4/HAC/H2O 88.8/6.3/4.9 88.8/6.3/4.9 88.8/6.3/4.9
mole % ratio
C2H4/HAC/H2O wt % ratio 84.2/12.8/3 84.2/12.8/3 84.2/12.8/3
C2H4/HAC mole ratio 14.2 14.2 14.2
Product Analysis
Products/Analysis Run No. 11 Run No. 12 Run No. 13
Ethylene Conversion 4.4 4.0 4.3
HAC Conversion 68 72 72
Product Selectivity (wt %)
EtAc 85.2 82.9 82.0
EtOH 3.7 3.7 3.9
DEE 10.5 13.0 13.6
Acetaldehyde 0.0 0.0 0.0
Oligomers 0.6 0.4 0.5
Others 0.01 0.02 0.07
EtAc Yield 58 60 59
EtAc STY (g/Lcat/h) 203 215 210
Carbon Balance (mol %) 102 103 103
Oxygen Balance (mol %) 87 87 89
Mass Balance 101 102 102
Water recovered (%) 43 39 42
TABLE 5
Run Conditions: (5 Mole % Water added to feed) using Catalyst 3:
Parameters Run No. 14 Run No. 15 Run No. 16
HOS 16-19 40-43 112.5-115.5
Temperature (° C.)
Applied 180 180 180
Bed (T/M/B) 179.1/191/ 179.1/190.5/ 179.2/190/
183.2 183.5 183.8
Pressure (Kpa) 1000 1000 1000
Total feed GHSV/h (@ STP) 980 980 980
C2H4 GHSV/h 866 866 866
HAC GHSV/h 64 64 64
H2O GHSV/h 50 50 50
C2H4 (g/Lcat/h) 1083 1083 1083
HAC (g/Lcat/h) 170 170 170
H2O (g/Lcat/h) 40 40 40
Feed contact time 4 4 4
[1/GHSV](secs)
C2H4/HAC/H2O 88.4/6.5/5.1 88.4/6.5/5.1 92.3/6.7/1.0
mole % ratio
C2H4/HAC/H2O wt % ratio 83.7/13.2/3.1 83.7/13.2/3.1 86/13.4/0.6
C2H4/HAC mole ratio 13.6 13.6 13.6
Product Analysis
Products/Analysis Run No. 14 Run No. 15 Run No. 16
Ethylene Conversion 6.6 7.6 6.3
HAC Conversion 86 85 83
Product Selectivity (wt %)
EtAc 73.4 74.0 73.2
EtOH 3.7 3.7 3.5
DEE 22.0 21.5 22.9
Acetaldehyde 0.0 0.0 0.0
Oligomers 0.6 0.7 0.5
Others 0.2 0.1 0.0
EtAc Yield 63 63 60
EtAc STY (g/Lcat/h) 219 221 224
Carbon Balance (mol %) 106 104 105
Oxygen Balance (mol %) 103 101 95
Mass Balance 105 104 104
Water recovered (%) 40 40 36
TABLE 6
Run Conditions: (5 Mole % Water added to feed) using Catalyst 3:
Parameters Run No. 17 Run No. 18 Run No. 19
HOS 160.5-163.5 208.5-211.5 285.5-288.5
Temperature (° C.)
Applied 180 180 180
Bed (T/M/B) 179.2/190/ 179.3/190/ 179.3/190/
184.1 184.3 184.2
Pressure (Kpa) 1000 1000 1000
Total feed GHSV/h (@ STP) 980 980 980
C2H4 GHSV/h 866 866 866
HAC GHSV/h 64 64 64
H2O GHSV/h 50 50 50
C2H4 (g/Lcat/h) 1083 1083 1083
HAC (g/Lcat/h) 170 170 170
H2O (g/Lcat/h) 40 40 40
Feed contact time 4 4 4
[1/GHSV](secs)
C2H4/HAC/H2O 88.4/6.5/5.1 88.4/6.5/5.1 88.4/6.5/5.1
mole % ratio
C2H4/HAC/H2O wt % ratio 83.7/13.2/3.1 83.7/13.2/3.1 83.7/13.2/3.1
C2H4/HAC mole ratio 13.6 13.6 13.6
Product Analysis
Products/Analysis Run No. 17 Run No. 18 Run No. 19
Ethylene Conversion 8.8 8.7 8.4
HAC Conversion 85 86 88
Product Selectivity (wt %)
EtAc 73.2 73.0 73.7
EtOH 3.6 3.9 3.7
DEE 22.6 22.6 22.1
Acetaldehyde 0.0 0.0 0.0
Oligomers 0.5 0.5 0.5
Others 0.1 0.1 0.1
EtAc Yield 62 63 65
EtAc STY (g/Lcat/h) 217 217 225
Carbon Balance (mol %) 104 104 104
Oxygen Balance (mol %) 103 103 103
Mass Balance 103 104 104
Water recovered (%) 40 41 38
TABLE 7
Run Conditions: (5 Mole % Water added to feed) using Catalyst 3:
Parameters Run No. 20 Run No. 21* Run No. 22*
HOS 375.5-378.5 448.5-451.5 472.5-475.5
Temperature (° C.)
Applied 180 180 180
Bed (T/M/B) 179.3/190/ 179.3/186.5/ 179.3/186.5/
184.4 183.4 183.4
Pressure (Kpa) 1000 1000 1000
Total feed GHSV/h 980 1001 1001
(@ STP)
C2H4 GHSV/h 866 866 866
HAC GHSV/h 64 64 64
H2O GHSV/h 50 50 50
DEE GHSV/h 0 21 21
C2H4 (g/Lcat/h) 1083 1083 1083
HAC (g/Lcat/h) 170 170 170
H2O (g/Lcat/h) 40 40 40
DEE (g/Lcat/h) 0 71 71
Feed contact time 3.7 3.6 3.6
[1/GHSV](secs)
C2H4/HAC/H2O/DEE 88.4/6.5/5.1§ 86.5/6.4/2.1§ 86.5/6.4/5/2.1
mole % ratio
C2H4/HAC/H2O/DEE 83.7/13.2/3.1§ 79.4/12.5/2.9/ 79.4/12.5/2.9/
wt % ratio 5.2 5.2
C2H4/HAC mole ratio 13.6 13.6 13.6
Product Analysis
Products/Analysis Run No. 20 Run No. 21 Run No. 22
Ethylene Conversion 8.7 2.7 2.4
HAC Conversion 85 81 80
Product
Selectivity (wt %)
EtAc 74.1 71.9 70.8
EtOH 3.6 5.0 5.4
DEE 21.6 22.9 23.3
Acetaldehyde 0.0 0.0 0.0
Oligomers 0.5 0.2 0.5
Others 0.1 0.0 0.0
EtAc Yield 63 59 57
EtAc STY (g/Lcat/h) 226 226 222
Carbon Balance 103 105 105
(mol %)
Oxygen Balance 98 101 98
(mol %)
Mass Balance 102 105 104
Water recovered (%) 38 60 63
*co-fed additionally with 2 Mole % DEE.
§No diethyl ether used in this Run
TABLE 8
Run No. 23 Run No. 24
Run Conditions: (5 Mole % Water + 2 Mole % DEE added to feed)
using Catalyst 3:
Parameters
HOS 479.5-500.5 544.5-547.5
Temperature (° C.)
Applied 180 180
Bed (T/M/B) 179.3/186.5/183.4 179.4/187/183.4
Pressure (Kpa) 1000 1000
Total feed GHSV/h (@ STP) 1001 1001
C2H4 GHSV/h 866 866
HAC GHSV/h 64 64
H2O GHSV/h 50 50
DEE GHSV/h 21 21
C2H4 (g/Lcat/h) 1083 1083
HAC (g/Lcat/h) 170 170
H2O (g/Lcat/h) 40 40
DEE (g/Lcat/h) 71 71
Feed contact time [1/GHSV](secs) 3.6 3.6
C2H4/HAC/H2O/DEE mole % ratio 86.5/6.4/5/2.1 86.5/6.4/5/2.1
C2H4/HAC/H2O/DEE wt % ratio 79.4/12.5/2.9/5.2 79.4/12.5/2.9/5.2
C2H4/HAC mole ratio 13.6 13.6
Product Analysis
Products/Analysis
Ethylene Conversion 1.4 1.3
HAC Conversion 84 82
Product
Selectivity (wt %)
EtAc 70.6 71.1
EtOH 5.1 5.2
DEE 23.9 23.5
Acetaldehyde 0.0 0.0
Oligomers 0.3 0.3
Others 0.0 0.0
EtAc Yield 59 58
EtAc STY (g/Lcat/h) 226 224
Carbon Balance (mol %) 107 106
Oxygen Balance (mol %) 103 99
Mass Balance 106 105
Water recovered (%) 61 63
TABLE 9
LIQUID PRODUCT DATA
GCMS
180° C., 1000 Kpa (10 barg), ethylene/acetic acid = 14
Run No.
Organics (% by Wt) 7 17 23
Water (mole % in feed) 1 5 5
(+2% DEE)
Acetic acid (unreacted feed) 52.3 21.2 16.3
Ethyl acetate 46.5 67.3 69
Diethylether 0.05 3 3.3
Ethanol 0.65 7.8 11
Acetaldehyde 0.002 0.04 0.009
C6 oligomers 0.0015 0 0
C8 oligomers 0.0055 0 0
Miscellaneous oxygenates 0.0065 0 0
Aromatic hydrocarbons 0.045 0 0
Unknowns 0.11 0.01 0
BALANCE: others
(Hydrocarbons & oxy
compounds)
Example 2
Catalyst Preparations
Catalyst 4. 12-Tungstophosphoric acid [H3PW12O40.24H2O] (175 g) was dissolved in distilled water (250 ml). Lithium nitrate [LiNO3.2H2O] (0.652 g) was dissolved in distilled water (˜5 ml). The lithium nitrate solution was added dropwise to the tungstophosphoric acid solution to form Solution “A”.
Solution “A” was added to pelleted silica support (Grace 1371 grade, 1-3 mm, 99.5 g, ex W R Grace) and left to soak over 24 hours with occasional stirring in order to impregnate the silica with the tungstophosphoric acid catalyst. After this duration, excess solution “A” was decanted and filtered off. The resultant catalyst impregnated support was then dried in flowing nitrogen gas initially at 150° C. for 3 hours and then raised to 200° C. and maintained at that temperature for 5 hours. The supported catalyst so formed was then left in a desiccator to cool and was finally reweighed. The resultant supported catalyst had a final weight of 164.4 g, a net catalyst loading of 64.9 g and had the formula Li0.1H2.9PW12O40.24H2O/SiO2 corresponding to a loading of 255 g/l.
Catalyst 4. Pelleted silica support (Grace 1371 grade, 1-3 mm, 70 g, ex W R Grace) was soaked in a solution (250 ml) of 12-tungstosilicic acid [H4SiW12O40.26H2O] (65.53 g in distilled water) for 24 hours with intermittent stirring in order to impregnate the support with the catalyst. Thereafter the excess solution of the tungstosilicic acid was removed by decantation and filtration. The resultant catalyst impregnated support was then dried overnight under flowing nitrogen at 120° C. The dried supported catalyst so formed was cooled in a desiccator and had a final weight of 86.2 g, a net catalyst loading of 16.2 g and had the formula H4SiW12O40.26H2O/SiO2 corresponding to a loading of 92 g/l.
The above catalysts were used to esterify ethylene with acetic acid. The relative amounts of each of these catalysts used, their bed size and bed length in performing the esterification reaction were as follows:
Parameter Catalyst 4 Catalyst 5
Volume (cm3) 25 25
Weight (g) 15.5 11.2-11.4
Pellet size (mm) 1-2 1-2
(Table 11) &
0.5-1  
(Tables 12, 13 and 14)
Bed length 8.5 8.75
TABLE 10
Run No. 25 Run No. 26 Run No. 27
(Catalyst 4-15.5 g)
Run Conditions:
Parameters
HOS 1-3 19-21 25-27
Temperature (° C.)
Applied 170 170 170
Bed (T/M/B) 173.5/—/170.5 172/—/169 172/—/169
Pressure (Kpa) 1000 1000 1000
Total feed GHSV/h 979 979 979
(@ STP)
C2H4 GHSV/h 905 905 905
HAC GHSV/h 65 65 65
H2O GHSV/h 9 9 9
C2H4 (g/Lcat/h) 1131 1131 1131
HAC (g/Lcat/h) 173 173 173
H2O (g/Lcat/h) 8 8 8
Feed contact time 4 4 4
[1/GHSV](secs)
C2H4/HAC/H2O mole 92.4/6.6/1.0 92.4/6.6/1.0 92.4/6.6/1.0
% ratio
C2H4/HAC/H2O wt % ratio 86.2/13.2/0.6 86.2/13.2/0.6 86.2/13.2/0.6
C2H4/HAC mole ratio 14.0 14.0 14.0
Product Analysis (Table 10 continued)
Products/Analysis
HAC Conversion 51 47 45
Product Selectivity (wt %)
EtAc 89.7 98.0 97.7
EtOH 0.5 0.5 0.4
DEE 0.9 0.7 1.0
Acetaldehyde 0.0 0.0 0.0
Oligomers 7.0 0.4 0.7
Others 1.90 0.49 0.26
EtAc Yield 45 46 44
EtAc STY (g/Lcat/h) 128 122 118
Carbon Balance (mol %) 102 102 105
Oxygen Balance (mol %) 86 89 100
Mass Balance 101 101 104
Water recovered (%) 90 70 81
TABLE 11
Run No. 28 Run No. 29 Run No. 30
(Catalyst 5-11.3 g)
Run Conditions:
Parameters
HOS 1-2 17-20 21-24
Temperature (° C.)
Applied 170 170 170
Bed (T/M/B) 176/—/174 173/—/170 173/—/170
Pressure (Kpa) 1000 1000 1000
Total feed GHSV/h (@ STP) 980 980 980
C2H4 GHSV/h 905 905 905
HAC GHSV/h 66 66 66
H2O GHSV/h 9 9 9
C2H4 (g/Lcat/h) 1131 1131 1131
HAC (g/Lcat/h) 177 177 177
H2O (g/Lcat/h) 8 8 8
Feed contact time 4 4 4
[1/GHSV](secs)
C2H4/HAC/H2O mole % ratio 92.3/6.7/1.0 92.3/6.7/1.0 92.4/6.6/1.0
C2H4/HAC/H2O wt % ratio 85.9/13.5/0.6 85.9/13.5/0.6 86.2/13.2/0.6
C2H4/HAC mole ratio 13.7 13.7 13.7
Product Analysis:
Products/Analysis
HAC Conversion 62 66 64
Product Selectivity (wt %)
EtAc 86.0 97.3 97.6
EtOH 2.4 0.4 0.4
DEE 3.3 1.8 1.4
Acetaldehyde 0.0 0.0 0.0
Oligomers 2.4 0.3 0.6
Others 5.9 0.1 0.1
EtAc Yield 53 65 62
EtAc STY (g/Lcat/h) 151 180 171
Carbon Balance (mol %) 101 104 105
Oxygen Balance (mol %) 98 95 99
Mass Balance 101 103 105
Water recovered (%) 70 69 67
TABLE 12
Run No. 31 Run No. 32 Run No. 33
(Catalyst 5-11.2 g)
Run Conditions:
Parameters
HOS 19.25-22.5 23-26 43.25-46.25
Temperature (° C.)
Applied 170 170 180
Bed (T/M/B) 172.5/176/— 172.5/175.5/— 182/187/—
Pressure (Kpa) 1000 1000 1000
Total feed GHSV/h 980 980 980
(@ STP)
C2H4 GHSV/h 905 905 905
HAC GHSV/h 66 66 66
H2O GHSV/h 9 9 9
C2H4 (g/Lcat/h) 1131 1131 1131
HAC (g/Lcat/h) 177 177 177
H2O (g/Lcat/h) 8 8 8
Feed contact time 4 4 4
[1/GHSV](secs)
C2H4/HAC/H2O mole % 92.3/6.7/1.0 92.3/6.7/1.0 92.3/6.7/1.0
ratio
C2H4/HAC/H2O wt % ratio 86/13.4/0.6 86/13.4/0.6 86/13.4/0.6
C2H4/HAC mole ratio 13.7 13.7 13.7
Product Analysis:
Products/Analysis
HAC Conversion 72 72 72
Product Selectivity (wt %)
EtAc 96.0 94.4 94.9
EtOH 0.5 0.5 0.7
DEE 2.9 2.7 3.3
Acetaldehyde 0.0 0.0 0.0
Oligomers 0.4 1.6 0.7
Others 0.2 0.3 0.8
EtAc Yield 69 68 78
EtAc STY (g/Lcat/h) 203 194 210
Carbon Balance (mol %) 101 103 108
Oxygen Balance (mol %) 91 97 104
Mass Balance 100 103 108
Water recovered (%) 47 48 48
TABLE 13
Run No. 34 Run No. 35 Run No. 36
(Catalyst 5-11.2 g)
Run Conditions:
Parameters
HOS 47-50 67.25-70.25 71-74
Temperature (° C.)
Applied 180 190 190
Bed (T/M/B) 181.5/186.5/— 191.5/196/— 191.5/195.5/—
Pressure (Kpa) 1000 1000 1000
Total feed GHSV/h 980 980 980
(@ STP)
C2H4 GHSV/h 905 905 905
HAC GHSV/h 66 66 66
H2O GHSV/h 9 9 9
C2H4 (g/Lcat/h) 1131 1131 1131
HAC (g/Lcat/h) 177 177 177
H2O (g/Lcat/h) 8 8 8
Feed contact time 4 4 4
[1/GHSV](secs)
C2H4/HAC/H2O mole 92.3/6.7/1.0 92.3/6.7/1.0 92.3/6.7/1.0
% ratio
C2H4/HAC/H2O wt % 86/13.4/0.6 86/13.4/0.6 86/13.4/0.6
ratio
C2H4/HAC mole ratio 13.7 13.7 13.7
Product Analysis:
Products/Analysis
HAC Conversion 79 74 72
Product
Selectivity (wt %)
EtAc 95.2 94.7 94.9
EtOH 0.7 0.7 0.7
DEE 3.2 2.8 2.2
Acetaldehyde 0.0 0.0 0.0
Oligomers 0.6 1.4 1.3
Others 0.2 0.3 0.8
EtAc Yield 75 70 68
EtAc STY (g/Lcat/h) 206 202 191
Carbon Balance 105 102 104
(mol %)
Oxygen Balance 102 94 99
(mol %)
Mass Balance 105 102 104
Water recovered (%) 47 52 54
TABLE 14
Run No. 37 Run No. 38 Run No. 39
(Catalyst 5-11.4 g)
Run Conditions:
Parameters
HOS 19-22 44-47 68.75-71.75
Temperature
(° C.)
Applied 180 180 180
Bed (T/M/B) 181.5/186/182.5 181.5/185/182 181.3/184.5/181.2
Pressure (Kpa) 1000 1000 1000
Total feed 980 980 980
GHSV/h
(@ STP)
C2H4 GHSV/h 905 905 905
HAC GHSV/h 66 66 66
H2O GHSV/h 9 9 9
C2H4 (g/Lcat/h) 1131 1131 1131
HAC (g/Lcat/h) 177 177 177
H2O (g/Lcat/h) 8 8 8
Feed contact time 4 4 4
[1/GHSV](secs)
C2H4/HAC/H2O 92.3/6.7/1.0 92.3/6.7/1.0 92.3/6.7/1.0
mole % ratio
C2H4/HAC/H2O 86/13.4/0.6 86/13.4/0.6 86/13.4/0.6
wt % ratio
C2H4/HAC mole 13.7 13.7 13.7
ratio
Product Analysis:
Products/Analysis
HAC Conversion 71 64 60
Product
Selectivity (wt %)
EtAc 95.9 97.2 97.8
EtOH 0.7 0.6 0.5
DEE 2.3 1.8 1.3
Acetaldehyde 0.0 0.0 0.0
Oligomers 0.8 0.3 0.3
Others 0.3 0.1 0.0
EtAc Yield 68 63 59
EtAc STY 194 183 164
(g/Lcat/h)
Carbon Balance 100 100 100
(mol %)
Oxygen Balance 94 89 93
(mol %)
Mass Balance 100 99 99
Water recovered 53 56 62
(%)

Claims (27)

1. A process for the production of lower aliphatic esters said process comprising reacting a lower olefin and a di-ether with a saturated lower aliphatic monocarboxylic acid in the vapour phase in the presence of a free acid silico-tungstic heteropolyacid catalyst supported on a siliceous support characterized in that an amount of water in the range from 1-10 mole % based on the total of the olefin, aliphatic mono-carboxylic acid and water is added to the reaction mixture during the reaction and the amount of di-ether is in the range from 1 to 6 mole % based on the total reaction mixture comprising the olefin, aliphatic carboxylic acid, water, and di-ether.
2. A process according to claim 1 wherein the amount of water added is in the range from 1 to 7 mole % based on the total of the olefin, aliphatic monocarboxylic acid and water.
3. A process according to claim 1 wherein the amount of water added is in the range from 1 to 5 mole % based on the total of the olefin, aliphatic monocarboxylic acid and water.
4. A process according to claim 1 wherein the heteropolyacid catalyst is supported on a siliceous support which is in the form of extrudates or pellets, said siliceous support having an average pore radius of 30 to 100 Å.
5. A process according to claim 4 wherein the siliceous support is derived from an amorphous, non-porous synthetic silica.
6. A process according to claim 4 wherein the siliceous support is derived from fumed silica produced by flame hydrolysis of SiCl4.
7. A process according to claim 4 wherein the silica support is in the form of pellets or beads or are globular in shape having an average particle diameter in the range from 2 to 10 mm, a pore volume in the range from 0.3-1.2 ml/g, a crush strength of at least 2 Kg force and a bulk density of at least 380 g/l.
8. A process according to claim 4 wherein the siliceous support has at least 99% w/w purity.
9. A process according to claim 4 wherein the siliceous support is a pelleted silica support which has an average bulk density of about 0.39 g/ml, an average pore volume of about 1.15 ml/g and an average particle size ranging from about 0.1-3.5 mm.
10. A process according to claim 9 wherein the pelleted silica support is used as such or after crushing to an average particle size in the range from 0.5-2 mm to support the heteropolyacid catalyst.
11. A process according to claim 1 wherein the heteropolyacids have a molecular weight e.g. in the range from 700-8500 and include dimeric complexes.
12. A process according to claim 4 wherein the amount of heteropolyacid deposited/impregnated on the support for use in the esterification reaction is in the range from 10 to 60% by weight based on the total weight of the heteropolyacid and the support.
13. A process according to claim 1 wherein the olefin reactant used is ethylene, propylene or mixtures thereof.
14. A process according to claim 1 wherein the saturated, lower aliphatic mono-carboxylic acid reactant is a c1-C4 carboxylic acid.
15. A process according to claim 1 wherein the aliphatic mono-carboxylic acid reactant is acetic acid.
16. A process according to claim 1 wherein the reaction mixture has a molar excess of the olefin reactant with respect to the aliphatic mono-carboxylic acid reactant.
17. A process according to claim 1 wherein the mole ratio of olefin to the lower carboxylic acid in the reaction mixture is in the range from 1:1 to 15:1.
18. A process according to claim 1 wherein the mole ratio of olefin to the lower carboxylic acid in the reaction mixture is in the range from 10:1 to 14:1.
19. A process according to claim 1 wherein the reaction is carried out in the vapour phase above the dew point of the reactor contents comprising the reactant acid, any alcohol formed in situ, the product ester and water.
20. A process according to claim 1 wherein the supported heteropolyacid catalyst is used as a fixed bed which is in the form of a packed column.
21. A process according to claim 1 wherein the heteropolyacid catalyst is further modified by the addition of phosphoric acid or other mineral acids thereto.
22. A process according to claim 1 wherein the vapours of the reactant olefins and acids are passed over the catalyst at a GHSV in the range of 100 to 5000 per hour.
23. A process according to claim 1 wherein the esterification reaction is carried out at a temperature in the range from 150°-200° C. using a reaction pressure which is at least 400 KPa.
24. A process according to claim 1 wherein the reaction mixture is dosed with a the di-ether which corresponds to the comprises a by-product di-ether formed in situ during the reaction from the reactant olefin which and the di-ether is recovered and recycled to the reaction mixture.
25. A process according to claim 24 wherein the amount of di-ether recycled is in the range from 1 to 6 mole percent based on the total reaction mixture comprising the olefin, the aliphatic carboxylic acid, water and di-ether.
26. A process according claim 24 wherein the di-ether is diethyl ether.
27. A process according to claim 24 wherein the di-ether is an unsymmetrical ether.
US11/712,545 1995-08-02 2007-02-28 Ester synthesis Expired - Lifetime USRE41341E1 (en)

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GBGB9515813.5A GB9515813D0 (en) 1995-08-02 1995-08-02 Ester synthesis
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GB9603770 1996-02-22
GB9613227 1996-06-25
GBGB9613227.9A GB9613227D0 (en) 1996-06-25 1996-06-25 Ester synthesis
US08/687,811 US5861530A (en) 1995-08-02 1996-07-26 Ester synthesis
US11/712,545 USRE41341E1 (en) 1995-08-02 2007-02-28 Ester synthesis

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