Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
  • C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
  • C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
  • C07C29/143—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of ketones
  • C07C29/145—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of ketones with hydrogen or hydrogen-containing gases
• • 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
  • C07C29/147—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 carboxylic acids or derivatives thereof
  • C07C29/149—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 carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
• • 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
  • C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
  • C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
  • C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
  • C07C31/18—Polyhydroxylic acyclic alcohols
  • C07C31/20—Dihydroxylic alcohols
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
  • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
  • C07C51/31—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation of cyclic compounds with ring-splitting
  • C07C51/313—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation of cyclic compounds with ring-splitting with molecular oxygen
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C67/00—Preparation of carboxylic acid esters
  • C07C67/08—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides with the hydroxy or O-metal group of organic compounds

Definitions

• step a) The hydrogenation of a DCL is very complex, as many compounds are contained, which can interfere with the actual hydrogenation or are also hydrogenated, which can complicate the following work-up. It was not trivial, but surprising, that the hydrogenation of the aldehydes in step a) was carried out so selectively that the C6-hydroxycarboxylic acids contained in the DCL were not already converted to 1,6-hexanediol in this step. If this had been the case, the resulting 1,6-hexanediol would then be separated off in step d) of the process according to the invention together with the 1,4-cyclohexanediols and thus reduce the yield of 1,6-hexanediol.
• the esterification can be carried out without the addition of catalysts, preferably under the action of catalysts.
• catalysts preferably under the action of catalysts.
• low molecular weight alcohols are usually those having 1 to 10 carbon atoms, in particular alkanols having 1 to 8 carbon atoms into consideration.
• diols such as butanediol or pentanediol come into consideration in principle.
• the technically preferred alcohols to be used for the esterification are n- or i-butanol and especially methanol.
• the high-boiling mixture obtained in column 2 can additionally be reacted again with esterification alcohol ROH (R3), subsequently freed of excess alcohol ROH in a further column K 4 and in a column K 5 in high boilers containing the 1, 4-cyclohexanediols and a further ester mixture EF 'are separated the.
• This EF 'can for example be fed back into the column K2 together with the ester mixture EG.
• the catalytically active ruthenium is applied by known methods, preferably on prefabricated T ⁇ O2 as a carrier material.
• the ruthenium catalyst precursors are reduced by treatment with hydrogen-containing gas, preferably at temperatures above 100 0 C.
• the catalysts are preferably before use in the inventive process at temperatures of 0 to 50 0 C, preferably at room temperature to mix with oxygen-containing gas mixtures, preferably passivated with air-nitrogen mixtures. It is also possible to incorporate the catalyst into the hydrogenation reactor in oxidic form and to reduce it under reaction conditions.
• the invention particularly preferred catalyst has a ruthenium content of 0.01 to 10 wt .-%, preferably from 0.1 to 6, based on the total weight of the catalyst of catalytically active metal and carrier on.
• the catalyst of the invention may have a sulfur content of 0.01 to 1 wt .-%, based on the total weight of the catalyst, wherein the sulfur determination is carried out coulometrically.
• the hydrogenation catalysts may be suspended in the reaction mixture. It is preferred to arrange them firmly in the hydrogenation reactor.
• the hydrogenation can be carried out batchwise or, preferably, continuously.
• the reaction mixture can be passed over the catalyst in bottom or trickle mode.
• the hydrogenation can be carried out in a single reactor or in two reactors connected in series. If two reactors are used, the two reactors may contain the same catalyst or two different catalysts. The two reactors may differ in the hydrogenation temperature and the hydrogen partial pressure.
• the dewatering (stage 2) in step b) can be carried out, for example, with a membrane system, or preferably by a distillation apparatus in which at 10 to 25O 0 C, preferably 20 to 200 0 C, particularly preferably 30 to 200 0 C and a pressure of 1 to 1500 mbar, more preferably 5 to 1 100 mbar, very particularly preferably 20 to 1000 mbar of water overhead and higher monocarboxylic acids, dicarboxylic acids and 1, 4-cyclohexanediols are separated off via bottom.
• the bottom temperature is preferably chosen so that the bottom product can be removed liquid.
• the water content in the bottom of the column can be from 0.01 to 10% by weight, preferably from 0.01 to 5% by weight, particularly preferably from 0.01 to 1% by weight.
• solid catalysts are acidic or super acidic materials, e.g. acidic and super acidic metal oxides such as SiC “2, Al2O3, SnC” 2, ZrC “2, phyllosilicates or zeolites, all of which may be doped with mineral acid residues such as sulfate or phosphate for acid amplification, or organic ion exchangers having sulfonic acid or carboxylic acid groups.
• the solid catalysts can be arranged as a fixed bed or used as a suspension.
• the water formed in the reaction is conveniently used continuously, e.g. through a membrane or removed by distillation.
• Particularly suitable intermediates are the hydroxides and carbonates or hydro gen carbonates, so that alkali metal carbonates or ammonium carbonate are used as particularly preferred precipitants.
• Important for the preparation of the catalysts is the thermal treatment of the intermediates at temperatures between 500 0 C and 100O 0 C.
• the BET surface area of the catalysts is between 10 and 150 m 2 / g.
• the hydrogenation discharge consists essentially of 1, 6-hexanediol and the alcohol ROH. Further constituents, especially if the entire low-boiling stream of stage 5 was used, 1, 5-pentanediol, 1, 4-butanediol, 1, 2-cyclohexanediols and small amounts of monoalcohols having 1 to 6 carbon atoms, optionally ether and water.
• the esterification alcohol ROH In order to operate the process according to the invention as economically as possible, it is expedient to recover the esterification alcohol ROH and to use it again and again for esterification.
• the predominantly alcohol ROH-containing stream from stage 4 and / or 7 can be worked up in stage 12.
• a column is advantageously used in which components which boil easier than the alcohol ROH overhead, water and components which boil higher than the alcohol ROH, are separated off via bottom of the alcohol ROH, which is obtained in a side stream.
• the column is suitably operated at 500 to 5,000 mbar, preferably at 800 to 3,000 mbar.
• the esterification stream from stage 2 was distilled (1015 mbar, 65 0 C head temperature, to 125 0 C bottom temperature). Over the head, 7.0 kg were withdrawn. The bottom product was 6.8 kg.
• Example 2 step 1 was repeated, with the difference that was used as the catalyst Ru (0.5%) on activated carbon. The hydrogenation result was equivalent to Example 2.
• Example 2 stage 1 was repeated, with the difference that the catalyst used was Ni (10% on activated carbon at 150 ° C. and 50 bar) The hydrogenation result was equivalent to Example 2.

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• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
• Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
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• 2010
  • 2010-03-29 KR KR1020117026357A patent/KR20120005018A/ko not_active Abandoned
  • 2010-03-29 SG SG2011066388A patent/SG174392A1/en unknown
  • 2010-03-29 WO PCT/EP2010/054053 patent/WO2010115738A1/de not_active Ceased
  • 2010-03-29 ES ES10711879T patent/ES2415156T3/es active Active
  • 2010-03-29 CN CN201080015253.6A patent/CN102388009B/zh not_active Expired - Fee Related
  • 2010-03-29 US US13/257,496 patent/US8629306B2/en not_active Expired - Fee Related
  • 2010-03-29 JP JP2012503955A patent/JP5586686B2/ja not_active Expired - Fee Related
  • 2010-03-29 EP EP10711879.6A patent/EP2417088B1/de not_active Not-in-force
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