Classifications

• • 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
  • B01J23/80—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 zinc, cadmium or mercury
• • 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
  • C07C29/14—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 a —CHO group
  • C07C29/141—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 a —CHO group with hydrogen or hydrogen-containing gases

Definitions

• This invention relates generally to a heterogeneous process for the liquid phase hydro- genation of aldehydes to the corresponding alcohols using reduced form of CuO/ZnO catalyst in the presence of a metal from Group IIIA of the Periodic Table such as aluminium. More particularly, this invention relates to the hydrogenation of hydroxypivalaldehyde to neopen- tylglycol.
• Aldehydes and corresponding primary alcohols are two general classes of organic compounds. There are several methods known in any textbook of organic chemistry and in patent literature for the conversion of aldehydes to the corresponding primary alcohols, such as chemical reduction methods using alkali or alkaline earth metal-derived borohydrides or aluminium hydrides and metal catalyzed-hydrogenation. Chemical reduction processes are seldom commercially viable. Usefulness of metal-catalytic processes is determined by conversion of aldehydes especially in presence of harmful impurities such as amines or other bases, selectivity of primary alcohol products, reaction conditions such as temperature and pressure, and even more importantly environmental issues caused by the metal catalysts.
• Some of the conventionally used metal catalysts although applied specifically for hydrogenation of hydroxypivaldehyde for making neopentyl glycol, may be equally effective to hydrogenate any aldehyde to the corresponding primary alcohol.
• This method is disclosed in Japanese Patent Publication Nos. 33169/1974, 17568/1678, U.S. Pat. Nos. 1,048,530, 1,219,162, 3,920,760, 4,021,496, West German Patent No. 1,014,089, and European Patent Nos. 44,421, 44,444.
• Raney nickel, Ni-Cr, Cu-Zn, Cu-Al, Cu-Cr and Cr-Ba catalysts are disclosed as catalysts for use in such hydrogenation reaction.
• 1,957,551 discloses the use of cobalt and nickel based catalysts in the hydrogenation of hydroxypivalaldehyde to neopentyl glycol, at high hydrogenation temperatures.
• Still another prior art WO 98/17614 (assigned to LG Chemicals, Korea) has described the use of Raney nickel in the hydrogenation of hydroxypivalaldehyde at low temperatures.
• these transition metal catalysts are deactivated by the presence of trace amounts of formaldehyde, or isobutyraldehyde, or trialkyl amine, which are present as impurities in the starting material hydroxypivalaldehyde.
• these catalysts can not be easily prepared and handled as they have to be used in the slurry form.
• T. Ninomiya et.al. have described in US Patent 4,933,473 (assigned to Mitsubishi Gas, Japan) the usage of a trimetallic (Pt/Ru/W) catalyst system for hydrogenation of hydroxypivalaldehyde. Although a 100% conversion of starting aldehyde and 100% selectivity of product are achieved at low reaction temperatures like 120°C, and at low pressure of 140-150 psig. a commercialization of this catalyst system is unlikely due to high cost of these metals.
• EP 484800 the use of CuO/ZnO in presence of ZrO is disclosed for hydrogenation of hydroxypivaldeyhde wherein the use of 25% percent equivalent (by weight) of the catalyst makes the process commercially unattractive.
• one of the objectives of the present invention is to overcome the difficulties and disadvantages encountered in the prior arts by providing a liquid-phase hydrogenation process utilizing a novel catalyst system comprising reduced form of CuO/ZnO in the presence of aluminium, a promoter for superior performance.
• the present invention provides a liquid-phase general catalytic hydrogenation process for aldehydes to the corresponding primary alcohols.
• the catalyst system comprises of copper oxide and zinc oxide with aluminium as a promoter.
• the process of this invention although general, is particularly useful for the hydrogenation of hydroxypivalaldehyde to neopentyl glycol. This process allows the hydrogenation to be carried out at moderate pressures such as 400-500 psig providing 100% conversion of aldehyde with 100% selectivity of the desired alcohol.
• the efficiency of the catalyst is retained even in the presence of deleterious impurities like trialkyl amine and quaternary ammonium hydroxide that may have been carried over to certain crude aldehyde products during their synthesis.
• This invention is particularly useful for making neopentyl glycol from hydroxypival- dehyde in 100% selectivity as this aldehyde does not decompose under hydrogenation conditions of this invention.
• the particular product, namely 2,2-dimethyl-l,3-dihydroxypropane (neopentyl glycol) of the process of the present invention is a valuable starting material for the manufacture of lubricants, plastics, surface coatings and synthetic resins, for example corresponding polyesters.
• the process of the invention may be a continuous process or a batch process.
• Ri, R , and R 3 individually could be straight chain or branched alkyl group containing 1 - 18 carbon atoms, or straight alkyl group containing 1-18 carbon atoms intervening with one or more hetero atoms such as oxygen, nitrogen, sulfur and phosphorus atoms, or alicyclic rings containing three or more carbon atoms when the ring(s) may or may not contain hetero atoms, or Ri, R , and R 3 together or alternately may form an alicyclic or aromatic rings, or any one or more of the R groups may contain one or more primary or secondary or tertiary alcohol group(s).
• G group can be a substituted or unsubstituted and fused or isolated aromatic or hetero- cyclic rings.
• G group can be a p-hydroxybenzyl group or a pyridinyl or furyl group.
• the catalyst may be prepared by any of the methods known in the art of forming a composite of copper oxide and zinc oxide.
• the catalyst may be prepared by fixing the separate oxides, by co-precipitation of the oxalates, carbonates, or acetates, followed by calcination.
• the co-precipitation method is preferred.
• the mixture of CuO and ZnO in the presence of the promoter metal is reduced by hydrogen of carbon monoxide at a temperature in the range of between 160° and 250°C for several hours, preferably 8 to 24 hours.
• the catalyst of the present invention can be used in a powder form or a tablet form obtained by compression molding. It can be employed in any reaction system such as a fixed bed system or a fluid bed system. After activation through hydrogenation according to the ordinary method, the catalyst is used in the hydrogenation reaction of the present invention.
• the mixture of CuO and ZnO and the promoter is reduced prior to its use as catalyst in the aldehyde hydrogenation process.
• Hydrogen or carbon monoxide, or mixtures thereof are used as the reducing agent.
• the hydrogen, carbon monoxide, or mixtures thereof are generally mixed with an inert gas such as steam, nitrogen, or combustion gas, to maintain the catalyst bed temperature and to carry away the heat of reduction.
• Reduction of the mixture of CuO and ZnO in presence of the promoter metal is complete when no more hydrogen is being reacted as shown by analysis of the inlet and outlet hydrogen.
• Complete reduction of the mixture occurs when the total amount of water produced in the reduction is equal to the stoichiometric value of water that should be produced when a given amount of copper oxide is reduced to copper. This value is about 36 gram of water per 450 gram of catalyst for a mixture of containing 35 weight percent of CuO.
• the catalyst is generally formed into pellets, tablets, or any other suitable shape prior to use providing suitable surface area, by conventional techniques.
• the process of the present invention is most conveniently carried out in batch operations although continuous or semi-continuous operations may also be employed.
• an alcoholic medium such as ethanol or methanol as a reaction solvent is used in such an amount that the hydroxypivaldehyde or any other aldehyde concentration is within the range of 10 to 80% by weight, preferably 15 to 60% by weight.
• an alcoholic medium such as ethanol or methanol as a reaction solvent
• the concentration is more than 80% by weight, Tischenko reaction between the hydroxypivaldehydes themselves occurs, resulting in neopentylglycol ester of hydroxypivalic acid as by-product, which is unsuitable for practical use.
• the hydrogenation can be carried out batchwise or continuously, advantageously at 100-200 °C, preferably from 120-180 °C, under a moderate pressure of from 20 psig to 500 psig, preferably from 400-500 psig.
• the catalyst is usually employed in an amount of from 2-12 percent by weight, preferably from 5-10 percent by weight, based on aldehyde, with a reaction time 1-4 hours, preferably 2-3 hours.
• the catalyst is reduced with hydrogen at pressure of 300-500 psig, preferably 400-500 psig and at a temperature of 100-200 °C, preferably 120-160°C
• the solvent is alcohol, preferably methanol or ethanol, especially methanol and water mixture.
• the atomic ratios of the components in the catalyst is from 0.8 - 1.25 of copper and 1.5-2.5 of zinc, more preferably 1.0-1.1 of copper and 1.8-2.0 of zinc.
• the atomic ratios of copper to aluminium is 1.0-1.5 of copper, 0.75-1.20 of aluminium, more preferably, 1.20-1.40 of copper and 0.90-1.10 of aluminium.
• the catalyst component used in the present invention is an environmental friendly, and easy to prepare and handle on an industrial scale. Furthermore, the presence of trialkylamines, formaldehyde will not deactivate this catalyst, and the hydrogenation can be carried out on crude hydroxypivaldehyde, thus avoiding the isolation and purification steps. According to this invention, even the presence of benzyl trimethylammonium hydroxide in the hydrogena- tion of hydroxypivaldehyde does not adversely affect the conversion of hydroxypivaldehyde, selectivity of the product neopentyl glycol and activity of the catalyst.
• the hydroxypivaldehyde conversion is 100%, and the selectivity of neopentyl glycol is also 100%), thus the desired product yield turns out to be quantitative and free from any unwanted impurity.
• aldehydes include saturated aldehydes like acetaldehyde, propionaldehyde, isobutyral- dehyde, n-butyraldehyde, isopentylaldehyde, n-pentyl aldehyde, 2-methyl pentyl aldehyde, crotonaldehyde, 2-ethyl hexaldehyde, methyl pentyl aldehyde, 2-ethyl butyraldehyde, and unsaturated C 3-8 aldehydes like acrolein, 2-ethyl propylacrolein, and benzaldehyde, furalde- hyde, pyridinylaldehyde and the like.
• the aldehyde may be in a substantially pure
• An oxo process or a cross-aldol condensation may obtain the aldehyde or mixture of aldehydes employed herein. A portion of the totality of the product mixture of an oxo process may be employed. Thus, the aldehyde(s) products or a portion of them may be separated from the product stream of an oxo process for hydrogenation by the process of this invention. For the purpose of providing an aldehyde feed, a conventional oxo product stream may be employed.
• aldehyde or mixture of aldehydes employed herein may also be obtained by processes other than oxo process, such as by oxidation of olefins or saturated hydrocarbons or by an aldol condensation.
• the process of the present invention comprises contacting a liquid-phase solution of aldehyde(s) of Formula (I) and (III) and hydrogen alone or in admixture with other gases (de- sirably gases inert to the aldehyde and the catalyst), with a solid catalyst comprising a reduced mixture of CuO and ZnO in presence of a promoter like Aluminium or any other metal of Group III of the Periodic Table.
• gases de- sirably gases inert to the aldehyde and the catalyst
• a solid catalyst comprising a reduced mixture of CuO and ZnO in presence of a promoter like Aluminium or any other metal of Group III of the Periodic Table.
• the gaseous mixtures containing hydrogen include inert gases such as nitrogen, or carbon dioxide.
• hydrogen-containing gas includes both substantially pure hydrogen gas as well as gaseous mixtures containing hydrogen.
• the mole ratio of contained hydrogen gas to aldehyde(s) may be generally from 15 to 40 and preferably, from 20 to 30.
• the hydrogenation process of the present invention is conducted at a temperature of between 110° and 180°C preferably between 130° and 170°C and at a pressure of between 20 and 500 psig, preferably between 400 and 500 psig.
• the alcohol product from the hydrogenation reaction in the batch process is isolated from the reaction mixture using the conventional methods.
• the catalyst is filtered off and reused for the next batch.
• the solvent from the filtrate is removed by a rotary evaporator.
• the recovered solvent is recycled in the next batch.
• the residual crude product is nearly pure, but is can be further purified by fractional distillation or fractional crystallization depending on the nature of the alcohol product.
• HYDROGENATION OF HYDROXYPIVALDEHYDE A 1.0 g quantity of the catalyst (CuO/ZnO/Aluminium oxide) in 50 ml methanol was placed in a 300 ml capacity Parr reactor. The contents were treated with hydrogen at 170°C, under pressure of 400-500 psig for 2-3 hrs. Cooled to room temperature, depressurized, followed by the addition of 10.0 g of hydroxypivaldehyde, in 50 ml methanol. Hydrogenation was carried out at 170°C, under a pressure of 400-500 psig, for 2-3 hrs. The conversion of hydroxypivaldehyde was 100%) providing 100% selectivity of neopentyl glycol, the desired alcohol product.
• a 1.0 g quantity of the catalyst (CuO/ZnO/ Aluminium oxide) in 50 ml methanol was placed in a 300 ml capacity Parr reactor. The contents were treated with hydrogen at 170°C, under pressure of 400-500 psig for 2-3 hrs. Cooled to room temperature, depressurized, followed by the addition of 10.0 g of benzaldehyde, in 50 ml of methanol. Hydrogenation was carried out at 170°C, under a pressure of 400-500 psig, for 2-3 hrs. The conversion of benzaldehyde was 100%) providing 100%) selectivity of benzyl alcohol, the desired alcohol product.
• a 1.0 g quantity of the catalyst (CuO/ZnO/ Aluminium oxide) in 50 ml methanol was placed in a 300 ml capacity Parr reactor. The contents were treated with hydrogen at 170°C, under pressure of 400-500 psig for 2-3 hrs. Cooled to room temperature, depressurized, followed by the addition of 10.0 g of 4-hydroxybenzaldehyde, in 50 ml of methanol. Hydrogenation was carried out at 170°C, under a pressure of 400-500 psig, for 2-3 hrs. The conversion of benzal- dehyde was 100%) providing 100% selectivity of 4-hydroxybenzyl alcohol, the desired alcohol product.
• a 1.0 g quantity of the catalyst (CuO/ZnO/ Aluminium oxide) in 50 ml of methanol was placed in a 300 ml capacity Parr reactor. The contents were treated with hydrogen at 170°C, under pressure of 400-500 psig for 2-3 hrs. Cooled to room temperature, depressurized, followed by the addition of 10.0 g of isobutyraldehyde, in 50 ml of methanol. Hydrogenation was carried out at 170°C, under a pressure of 400-500 psig, for 2-3 hrs. The conversion of isobutyraldehyde was 100%) providing 100%) selectivity of isobutyl alcohol, the desired alcohol product.
• a 1.0 g quantity of the catalyst (CuO/ZnO/ Aluminium oxide) in 50 ml of methanol was placed in a 300 ml capacity Parr reactor. The contents were treated with hydrogen at 170°C, under pressure of 400-500 psig for 2-3 hrs. Cooled to room temperature, depressurized, followed by the addition of 10.0 g of n-butyraldehyde, in 50 ml of methanol. Hydrogenation was carried out at 170°C, under a pressure of 400-500 psig, for 2-3 hrs. The conversion of n- butyraldehyde was 100%> providing 100% selectivity of n-butyl alcohol, the desired alcohol product.

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• 1999
  • 1999-10-20 EP EP99121002A patent/EP1094051B1/en not_active Expired - Lifetime
  • 1999-10-20 DE DE69908777T patent/DE69908777T2/de not_active Expired - Lifetime
• 2000
  • 2000-02-27 SA SA00201006A patent/SA00201006B1/ar unknown
  • 2000-08-25 MY MYPI20003929A patent/MY122647A/en unknown
  • 2000-10-18 CN CNB008144672A patent/CN1177784C/zh not_active Expired - Lifetime
  • 2000-10-18 JP JP2001531770A patent/JP4124414B2/ja not_active Expired - Lifetime
  • 2000-10-18 US US10/110,904 patent/US6600078B1/en not_active Expired - Lifetime
  • 2000-10-18 WO PCT/IB2000/001503 patent/WO2001028964A2/en not_active Ceased

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