PROCESS FOR THE PREPARATION OF OPTIONALLY ALKYL-SUBSTITUTED RESORCINOL AND CATALYST TO BE USED IN THIS PROCESS

Abstract: Preparation of optionally alkylsubstituted resorcinol by conversion of an ester of a 4-oxopentane-1-carboxylic acid in the gaseous state using a dehydrogenation catalyst in which one or more metals selected from the group consisting of platinum, palladium, ruthenium, iridium and rhodium on a carrier are used, with as carrier a combination of one or more oxides selected from the group consisting of silicon dioxides, aluminium oxide and titanium oxide and one or more oxides selected from the group consisting of thorium oxide and lanthanide oxides.

Description: PROCESS FOR THE PREPARATION OF OPTIONALLY ALKYL-SUBSTITUTED RESORCINOL AND CATALYST TO BE USED IN THIS PROCESS The invention relates to a process for the preparation of optionally alkyl-substituted resorcinol by conversion of an ester of optionally alkyl-substituted 4-oxopentane-l-carboxylic acid in the gaseous state using a dehydrogenation catalyst, and to the catalyst to be used in this process. This process has been described in United States Patent Specification 3,950,438. On further experimental examination of the methodology described in said patent specification it has been found that when applying known dehydrogenation catalysts, such as, for instance, platinum on carbon, the conversion of the ester in question and the resorcinol efficiency decrease fairly rapidly, for instance after an operating time of 40 hours, to a value that is unacceptable for practical purposes. The present invention provides a dehydrogenation catalyst allowing the efficiency and the conversion to be maintained for a long time at a value that is more suitable for practical purposes. The process according to the invention for the preparation of optionally alkyl-substituted resorcinol by conversion of an ester of optionally alkyl-substituted 4-oxopentane-1-carboxylic acid in the gaseous state using a dehydrogenation catalyst is characterized in that one or more metals selected from the group consisting of platinum, palladium, ruthenium, iridium and rhodium on a carrier is used as dehydrogenation catalyst, with as carrier a combination of one or more oxides selected from the group consisting of silicon dioxide, aluminium oxide and titanium oxide and one or more oxides selected from the group consisting of thorium oxide and lanthanide oxides. The process according to the invention can be carried out starting from various esters of the 4-oxopentane-l-carboxylic acid such as, for instance, alkyl-, cycloalkyl-, and phenyl-esters. Very suitable are alkyl-esters with an alkyl group containing up to 6 carbon atoms. In the process according to the invention a univalent alcohol is formed from the ester group, for instance methyl alcohol when methyl ester of said carboxylic acid is started from. The alcohol formed can be recovered from the reaction mixture and be used for the preparation of the starting product. Optionally, the starting product can be substituted by an alkyl group in the 1st, 2nd, 3rd and/or 5th positions. The total number of carbon atoms of these substituents will preferably not be chosen higher than 12, and the number of carbon atoms of one substituent preferably not higher than 6. The noble metal content of the catalyst according to the invention can be varied, for instance between 0.1 and 15 % by weight of noble metal. By preference a content of 0.5-5 % by weight of noble metal is used. As noble metal platinum is particularly suitable. The catalyst according to the invention can be used on a carrier chosen from various combinations of one or more oxides selected from the group consisting of silicon dioxide, aluminium oxide and titanium oxide and the other group of oxides in question. By preference the combination of silicon dioxide and thorium oxide is applied as carrier in a relative weight ratio of 1-80 grams of thorium oxide, in particular 5-15 grams of thorium oxide per 100 grams of silicon dioxide. The porosity of the silicon dioxide may vary. A good result can be obtained witb silicon dioxide of medium porosity, i.e. silicon dioxide the average pore radius of which is between 2 and 5 nanometers (measured by capillary condensation of nitrogen for the 1-30 nanometer range). The process according to the invention can be carried out in various ways. The gaseous starting product can be diluted with an inert gas such as, for instance, nitrogen and carbon dioxide and be contacted with the catalyst in the form of a fixed bed or a fluid bed. The gaseous starting product can also be contacted with the catalyst in the presence of hydrogen, which has a favourable influence upon the activity of the catalyst. The space velocity may be varied, for instance between 0.05 and 5 grams of ester per milliliter of catalyst per hour. Usually a space velocity of between 0.1 and 1.5 grams of ester per milliliter of catalyst is applied. The process according to the invention may be carried out at various reaction temperatures. By preference a temperature between 200 and 400 OC is applied. The gaseous reaction mixture obtained at such temperatures can be cooled, with the possibility of utilizing the heat to be discharged, to form a condensate, after which the desired product can be recovered from this condensate by fractionated distillation or extraction. Besides the desired product, the reaction mixture obtained contains non-converted ester, which can be recycled, and possibly also a small amount of the 4-oxopentane-l-carboxylic acid corresponding to the ester and/or the lactone of the acid in question. This small amount of the 4-oxopentane-l-carboxylic acid and/or the lactone can be separated off and be converted into the ester in question. It has, however, been found that recycling of the acid and/or lactone in question together with the non-converted ester in an amount of at most 0.4 moles of acid and/or lacton per mole of the ester to be passed over the catalyst does not have any adverse consequences. In the following examples the invention will be further elucidated. Catalyst preparation Silicon dioxide lumps (49.6 grams, diameter 3-8 mm, average pore radius 3.6 nm, type silicon dioxide gel M of the firm Hermann at Cologne, W. Germany) are, to avoid fracturing, immersed in a beaker filled with approximately 90 ml of acetone. Subsequently 100 ml of water is added whilst stirring, after which the lumps are filtered off and washed three times with water. The silicon dioxide thus moistened is then mixed with a solution of 11.8 grams of Th(N03)4 . 4 H20 in 60 ml of water in an evaporation dish. The mixture is evaporated on a water bath whilst 0 being stirred and subsequently dried for 1 hour at 110 C. The dried product is then calcined for 2 hours at 550 OC, The carrier obtained is subsequently mixed with a solution of 1.32 grams of H2PtCl6. 6 H20 in 50 ml of water, the mixture obtained is evaporated whilst being stirred and the evaporated product is dried for 16 hours at 110 OC. The dried product is finally introduced into a reactor (as described hereafter in the examples) and activated for 16 hours at 350 OC by passing hydrogen over it. The yield is 56 grams of catalyst containing 1 by weight of platinum and 11.4 % by weight of ThO2 (10 % by weight of Th). In a similar way other catalysts according to the invention can be prepared. The metal oxide required for the carrier can be obtained from various salts, for instance CeO2 from Ce(N03)2 . 6 H20 or Nd2O3 from NdCl3. Example 1 Through a vertical tubular reactor (18 mm in diameter and 400 mm in length), in which there is a zone of 25 ml (bulk volume) of catalyst, a gaseous mixture of nitrogen, hydrogen and methyl ester of 4-oxopentane-1-carboxylic acid is made to descend for about 845 hours. The catalyst zone is on both sides bounded by a zone of 25 ml of inert ceramic material. As catalyst, platinum on a carrier of silicon dioxide and thorium oxide (prepared and activated in the way indicated above, 1 % by weight of Pt, 10 % by weight of Th) is applied. The -gaseous mixture (4 moles of hydrogen and 2 moles of nitrogen per mole of methyl ester) is obtained by evaporating liquid methyl ester and mixing the vapour with hydrogen and nitrogen. Per milliliter (bulk volume) of catalyst 0.2 grams/hour of methyl ester are passed through. The first 400 hours the temperature of the catalyst is kept at 320 C, by means of a heating jacket around the reactor, and afterwards at 350 OC, The composition of the reaction mixture obtained is determined a number of times by passing the gas mixture obtained for some time, for instance 1 hour, through two coupled vessels, which are cooled to 0 C and -80 C repsectively, and analysing the condensed product thus obtained gas chromatographically. The weight and the composition of the condensed product obtained are given in the table below. This table also indicates the calculated conversion of the ester and the efficiencies of the products obtained as well as the operating time that has passed as soon as the gaseous reaction mixture is led through the cooled vessels. operating weight of composition (% by weight) efficiency (mol %) conversion % time product in recor- dihydro- phenol methyl resor- dihydro- phenol grams cinol resorcinol ester cinol resorcinol 43 16.2 24.6 4.2 5.4 34.9 36.4 6.2 9.4 71.7 89 8.1 20.5 4.6 3.9 46.4 38.7 8.5 8.6 59.9 185,5 27.8 16.3 4.5 2.6 56.2 36.9 9.9 6.9 50.7 235,5 4.0 17.7 4.9 2.8 58.9 40.1 10.9 7.4 49.5 334,5 9.2 14.5 4.2 2.2 60.8 35.1 10.4 6.2 29.8 402 5.6 33.1 4.6 4.3 40.0 50.3 6.9 7.7 68.3 500 5.0 26.0 5.4 3.0 45.1 45.9 9.4 6.2 60.8 596 9.6 24.1 5.6 2.8 47.1 48.1 10.9 6.5 58.3 741 4.5 20.4 5.6 2.0 54.5 46.3 12.6 5.2 51.4 859 6.3 20.4 5.4 3.2 49.3 41.7 10.9 7.6 56.5 Comparative example 1 The experiment described in Example 1 is repeated for about 115 hours at a catalyst temperature of 320 C with the same type of catalyst, but without ThO2 (1% by weight of Pt on silicon dioxide). After an operating time of 42 hours, the conversion of the methyl ester amounts to 27.6 %. Of the converted methyl ester 18.8 % has been converted into resorcinol, 8 % into dihydroresorcinol and 13 % into phenol. After an operating time of 114 hours the conversion of the methyl ester amounts to 17.3 %. Of the amount of methyl ester converted then 13 % has been converted into resorcinol, 17.7 7o into dihydroresorcinol and 18.5 % into phenol. Comparative example 2 The experiment described in Example 1 is repeated for about 42 hours at a catalyst temperature of 350 C with the same type of catalyst, but with carbon instead of silicon dioxide. After an operating time of 41 hours the conversion of the methyl ester amounts to 33 %. Of the methyl ester converted 4.9 % has been converted into resorcinol, 39.6 % into dihydroresorcinol and 3.8 % into phenol. During this experiment the weight of the catalyst appears to have increased by approximately 27 % as a result of tar deposition. Example II The experiment described in Example 1 is repeated for about 740 hours at a catalyst temperature of 350 C. In doing so, the amounts of hydrogen and nitrogen (expressed in moles per mole of ester) in the gaseous starting compound as well as the space velocity (expressed in grams of ester per ml of catalyst per hour) are varied some hours before the analytical measurements. The pertaining data and results have been tabulated below. operating space N2 H2 weight of composition (% by weight) efficiency (mole %) convertime velocity product resor- dihydro- phenol methyl resor- dihydro- phenol sion % in in cinol resor- ester cinol resorhours grams cinol cinol 41 0.17 4.0 8.0 7.2 24.3 2.0 31.9 9.5 22.7 1.8 35.0 93.6 66 0.17 4.0 8.0 7.8 14.8 1.9 30.3 15.9 18.3 2.4 44.0 86.9 89.5 0.17 8.0 16.0 8.6 27.7 3.7 18.5 15.4 27.3 3.6 21.3 89.7 256.5 0.17 8.0 16.0 6.0 41.4 8.2 8.9 27.3 38.9 7.6 9.8 83.6 353.5 0.17 8.0 16.0 4.0 39.5 8.5 8.4 27.4 31.6 6.7 7.0 85.6 378 0.5 4.0 8.0 20.4 19.5 8.8 2.5 56.3 45.6 20.2 6.9 49.9 425.5 0.5 4.0 8.0 31.4 16.8 8.0 1.9 62.0 45.1 21.1 6.1 44.0 569 0.5 4.0 8.0 20.2 14.2 8.5 1.5 61.3 39.0 23.0 4.7 43.7 593 1.0 2.0 4.0 25.0 8.4 7.6 0.7 72.5 35.5 31.6 3.5 29.9 665.5 1.0 2.0 4.0 68.9 7.3 7.5 0.6 74.8 32.2 32.5 2.9 28.5 689 1.0 3.0 6.0 28.1 6.8 7.3 0.6 75.6 30.4 32.0 2.9 28.1 713 1.0 3.0 6.0 68.4 6.5 7.5 0.6 76.4 24.4 27.7 2.4 31.2 738 1.0 1.0 2.0 20.0 6.3 7.5 0.5 75.2 25.1 25.7 2.3 30.2 Example III In the way described in Example I the isopropyl ester of 4-oxopentane-1-carboxylic acid is for approximately 75 hours converted at a catalyst temperature of 350 C, uwing the same type of catalyst as in Example I. Per mole of isopropyl ester 8 moles of hydrogen and 4 moles of nitrogen are used. The space velocity is 0.8 grams of ester per milliliter of catalyst per hour. After an operating time of 72 hours the conversion of the ester amounts to 45.3 %. Of the amount of ester converted 33.1 % has been converted into resorcinol, 27.7 % into dihydroresorcinol and 5.7 into phenol. Example IV In the way described in Example I the ethyl ester of 4-oxopentane-1-carboxylic acid is converted for about 760 hours at a catalyst temperature of 320 C, using the same type of catalyst as in Example I. The space velocity is 0.2 grams of ethylvester per milliliter of catalyst per hour. After an operating time of 480 hours, for 50 hours 6 moles of H2 per mole of ester are applied instead of 2 moles of N2 and 4 moles of H2 per mole of ester. The pertaining data and results have been tabulated below. operating weight of composition (% by weight) efficiency (mole %) conversion % time product resor- dihydro- phenol methyl resor- dihydro- phenol in in cinol resorcinol ester cinol resorcinol hours grams 40 3.74 22.8 1.7 8.0 25.4 30.3 2.2 12.5 81.0 138 8.23 27.6 3.1 6.9 39.6 45.6 3.9 13.4 68.7 185.5 4.8 20.2 2.7 5.4 50.1 54.4 7.2 17.1 51.6 233.5 38.2 19.6 3.1 5.7 46.3 38.6 6.0 13.2 61.2 353.5 24.0 18.9 3.7 5.1 51.5 38.8 7.5 12.2 57.5 406.5 4.6 18.2 3.0 5.4 52.4 46.8 7.6 16.1 57.6 476 13.6 16.1 3.5 4.1 54.4 37.6 8.0 11.3 53.0 504 3.2 15.8 3.1 6.7 49.9 26.3 5.1 13.1 63.4 522 11.8 14.5 2.9 6.7 50.4 31.2 6.1 16.7 57.0 547 4.5 17.0 3.3 4.6 55.2 29.6 7.6 12.6 52.8 613 4.4 16.1 3.2 4.4 56.4 38.0 7.4 12.0 51.9 636.5 4.2 14.9 3.5 4.1 59.0 43.2 10.1 13.8 44.0 756 4.5 13.1 3.1 3.1 62.2 35.9 8.4 9.9 45.7 Example V The experiment described in Example I is repeated for about 385 hours using as catalyst platinum on a carrier of silicon dioxide with CeO2 (1 % by weight of Pt and 5 % by weight of Ce). The space velocity is 0.2 grams of ester per milliliter of catalyst per hour. The first 190 hours 6.2 moles of N2 and 14.3 moles of H2 are used per mole of ester, and afterwards 3.9 moles of N2 and 7.8 moles H2. The first 335 hours the catalyst is kept at 350 C and afterwards at 320 OC. In the table below the results are indicated. operating weight of composition (% by weight) efficiency (mole %) conversion % time product resor- dihydro- phenol methyl resor- dihydro- phenol in in cinol resorcinol ester cinol resorcinol hours grams 41 2.6 21.6 1.5 22.7 12.0 18.7 1.3 22.9 92.7 115.5 4.1 25.4 3.4 13.7 30.1 33.8 4.4 21.3 76.6 161.5 4.5 24.9 3.9 9.4 33.0 39.4 6.0 17.5 71.5 187.5 4.3 21.2 3.0 13.1 24.5 31.5 4.4 22.9 76.9 210.5 3.7 27.3 3.5 11.7 31.4 36.8 4.6 18.5 75.5 311 4.9 27.4 3.5 12.0 26.3 33.1 4.2 16.9 80.5 311.5 5.6 28.0 4.2 9.1 31.2 41.4 6.0 15.8 73.9 353 8.5 13.4 3.9 4.1 57.1 29.0 8.3 10.4 51.5 383 4.7 13.6 4.0 4.2 57.6 39.9 11.5 14.4 45.3

Claims: CLAIMS 1. Process for the preparation of optionally alkyl-substituted resor cinol by conversion of an ester of optionally alkyl-substituted 4-oxopentane-1-carboxylic acid in the gaseous state using a dehydrogenation catalyst, this process being characterized in that one or more metals selected from the group consisting of platinum, palladium, ruthenium, iridium and rhodium on a carrier are used as dehydrogenation catalyst, with as carrier a combination of one or more oxides selected from the group consisting of silicon dioxide, aluminium oxide and titanium oxide and one or more oxides selected from the group consisting of thorium oxide and lanthanide oxides. 2. Process according to claim 1, characterized in that a dehydrogena tion catalyst is, used with a content of 0.5-5 % by weight of metal of said group of metals. 3. Process according to either claim 1 or 2, characterized in that platinum is used as metal. 4. Process according to any of the claims 1-3, characterized in that the combination silicon dioxide thorium oxide is used as carrier. 5. Process according to claim 4, characterized in that silicon dioxide of medium porosity is used. 6. Process according to either claim 4 or 5, characterized in that 5-15 grams of thorium oxide are used per 100 grams of silicon dioxide. 7. Process according to any of the claims 1-6, characterized in that the acid and/or lactone formed during the conversion of the ester is recycled and per mole of ester to be passed over the catalyst less than 0.4 moles of said acid and/or lactone are passed over the catalyst. 8. Dehydrogenation catalyst suitable for application in the process according to any of the claims 1-7, characterized in that in the catalyst platinum, silicon dioxide and thorium oxide are present. 9. Catalyst according to claim 8, characterized in that the catalyst contains 0.5-5 % by weight of platinum and 5-15 grams of thorium oxide per 100 grams of silicon dioxide. 10. Catalyst according to any of the claims 8 or 9, characterized in that the catalyst contains silicon dioxide of medium porosity.

Inventors: BOELENS, CHRISTIAAN, JANSSEN, PETRUS HUBERTUS JOSEPH, KLEUSKENS, ENGELINA CATHERINA, VAN DE MOESDIJK,  CORNELIS GERARDUS MARIA, VAN DE MOESDIJK, CORNELIS GERARDUS MARIA
Applicants: STAMICARBON B.V.
Application year: 1980
Main classification: C07C39
IPC codes: C07C37, C07C29