US3683035A - Process for manufacturing alcohols by oxidation of hydrocarbons - Google Patents

Process for manufacturing alcohols by oxidation of hydrocarbons Download PDF

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US3683035A
US3683035A US729035A US3683035DA US3683035A US 3683035 A US3683035 A US 3683035A US 729035 A US729035 A US 729035A US 3683035D A US3683035D A US 3683035DA US 3683035 A US3683035 A US 3683035A
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oxidation
hydrocarbon
phase
pipe
percent
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Jacob Alagy
Francois Bigache
Bernard Cha
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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    • 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
    • C07C29/48—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by oxidation reactions with formation of hydroxy groups
    • C07C29/50—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by oxidation reactions with formation of hydroxy groups with molecular oxygen only
    • C07C29/52—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by oxidation reactions with formation of hydroxy groups with molecular oxygen only in the presence of mineral boron compounds with, when necessary, hydrolysis of the intermediate formed
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2601/00—Systems containing only non-condensed rings
    • C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
    • C07C2601/14—The ring being saturated

Definitions

  • BY (4, 9 47m14' ATTORNEYS PROCESS FOR MANUFACTURING ALCOHOLS BY OXIDATION OFHYDROCARBONS It is known to oxidize linear or cyclic saturated hydrocarbons, in a liquid phase, in the presence of a boric acid (for example ortho-, metaor pyroboric acid), boric anhydride or a boric ester, or any other equivalent boron compound, to obtain boric esters of the alcohols corresponding to said hydrocarbons.
  • a boric acid for example ortho-, metaor pyroboric acid
  • boric anhydride or a boric ester or any other equivalent boron compound
  • Oxygen is usually employed in a concentration of l to 25 percent as a mixture with an inert gas such as nitrogen.
  • oxidation of cyclohexane provides for a cyclohexyl borate.
  • Other oxidizable hydrocarbons are those which contain from five to eight carbon atoms per molecule, for example hexane, heptane, octane, isooctane, cycloheptane, cyclooctane, methylcyclohexane and dimethylcyclohexanes (ortho-, metaor para-).
  • the oxidation temperature is usually between 100 and 220 C., preferably between 140 and 190 C., with a pressure which is sufficient to maintain a liquid phase, for example between 1 and 40 atmospheres.
  • boric acid may be recovered either directly in the solid state or as an aqueous solution which may be subjected to crystallization as well as an organic phase which contains the expected alcohol, usually together with a minor proportion of the corresponding ketone.
  • water or the mother-waters of a prior crystallization of boric acid may be used as hydrolysis agent.
  • the amount of water must be at least the stoichiometrical amount with respect to the hydrolysis reaction; usually 0.1 to 2 parts by volume of aqueous phase may be used for one part by volume of effluent from the oxidation zone, and the temperature is most often between 20 and 170 C.
  • the recovered boric acid may be re-used in another oxidation operation, preferably after dehydration.
  • the unconverted hydrocarbon may be recycled. lts recovery may be carried out by distillation of the organic phase after hydrolysis and saponification.
  • this distillation will be preceded by a partial distillation of the hydrocarbon (for example to 90 percent of the present hydrocarbon) by release of pressure on the liquid efiluent from the oxidation zone, before saponification and preferably also before hydrolysis.
  • a partial distillation of the hydrocarbon for example to 90 percent of the present hydrocarbon
  • the thus obtained vapor phase, after condensation', will be sent back to the oxidation reactors, whereas the liquid phase will be subjected to hydroly sis, saponification and distillation.
  • the object of this invention is to avoid the said inconvenience. It has been observed that a washing of the hydrocarbon contained in the vapors obtained during the release of pressure was necessary, said washing being carried out with a mineral base such as an oxide, a hydroxide or a carbonate of an alkali or alkali-earth metal, for example sodium hydroxide, ammonia, sodium carbonate, potassium carbonate, potassium hydroxide or calcium hydroxide, and followed by a washing with water. It appears that formic acid or any other light product separated during the release of pressure, if it is not rejected, results into a partial inhibition of the reaction.
  • a mineral base such as an oxide, a hydroxide or a carbonate of an alkali or alkali-earth metal, for example sodium hydroxide, ammonia, sodium carbonate, potassium carbonate, potassium hydroxide or calcium hydroxide
  • the excess of sodium hydroxide contained in the aqueous phase separated from the saponified liquid phase issuing from the release unit.
  • This basic solution contains oxidation products of value, for example cyclohexanol and cyclohexanone, and the organic liquid phase newly extracts these products which otherwise would be lost, thus resulting into a substantial yield loss in the unit.
  • the amount of mineral base will be advantageously at least that amount which would correspond to the neutralization of 50 percent of the acids present.
  • this base is preferably used in an amount corresponding to 110-300 percent of the theoretical amount corresponding to the neutralization of the acids, in order to realize simultaneously a saponification of the esters present. It is of little importance that this base be in the form of a concentrated or diluted aqueous solution.
  • the gaseous phase which is withdrawn through pipe 11 and condensed in the heat exchanger 4 is admixed in the neutralization column 5, with an alkaline solution from pipe 12.
  • the aqueous phase is withdrawn from the column through pipe 13, and the organic phase through pipe 14. The latter is admixed with water issuing from pipe 15 and introduced into the washing column 6.
  • the aqueous phase is withdrawn through pipe 16 and the organic phase through pipe 17.
  • This phase which consists essentially of unconverted hydrocarbon, is sent back to the oxidation step.
  • the liquid phase from the vaporization vessel 3 is withdrawn through pipe 18, is subjected to the usual treatment, i.e., hydrolysis and washing in the vessel 7 by means of an aqueous solution of boric acid or water, or a mixture of both, fed through pipe 19.
  • the aqueous phase which contains water-soluble components is sent through pipe 20 to the step wherein boric acid is recovered.
  • the organic phase is withdrawn through pipe 21 and saponified in vessel 8, the sodium hydroxide solution being fed through pipe 22 and diluted with the aqueous phase of pipe 16, issuing from the washing step of column 6.
  • the residual alkaline aqueous phase is withdrawn through pipe 12 and used to feed the neutralization column 5.
  • the organic phase which contains the oxidation products and a part of the unconverted hydrocarbon, is sent through pipe 23 to the separation step 9, for example by distillation, where the unconverted hydrocarbon issues through pipe 24 to be sent back to the oxidation step, the alcohol-ketone mixture being extracted through pipe 25.
  • Example 1 is given by way of comparison and forms no part of this invention.
  • the liquid phase issuing from the last vessel, which contains the oxidation products as well as the excess of boric acid, is subjected to a release of pressure down to 5 atmospheres at 120 C., the latter temperature being maintained by means of a heat exchanger.
  • the obtained vapor phase contains about 93 percent by weight of cyclohexane.
  • a minor proportion of the oxidation products is carried away about 8 percent by weight of the organic acids (essentially formic acid) which are present in the effluent of the last vessel as well as 10 percent of the cyclohexyl organic esters.
  • the total amount of vapor phase separated during this pressure release amounts to about 35 percent of the total effluent from the reaction vessels.
  • the condensate is sent back to the reaction vessels in order to be subjected to another oxidation step.
  • the aqueous phase from the saponification of the hydrolysis effluent is not used to carry out a neutralization of the condensate and thus is only rejected.
  • Example 1 is repeated, except that the condensed hydrocarbon is neutralized by means of a 0.2N sodium hydroxide solution which is used in an amount of 120 percent with respect to the amount corresponding to the theoretical neutralization of the acids, then it is washed with water before being recycled to the oxidation vessels.
  • the aqueous phase issued from the saponification of the hydrolysis effluent is not used, here again, to carry out the neutralization of the condensate. It is only rejected.
  • the molar yield of cyclohexanol cyclohexanone is 89 percent and the conversion has attained l 1 percent.
  • Example 1 is repeated, except that the condensed hydrocarbon is neutralized by means of the aqueous phase issued from the saponification of the hydrolysis efiluent.
  • This aqueous phase contains an excess of sodium hydroxide, which has not been consumed during the saponification, in an amount equal to that defined in Example 2.
  • the molar yield of cyclohexanol+cyclohexanone is 91 percent for a conversion rate of 1 1 percent.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US729035A 1967-05-29 1968-05-14 Process for manufacturing alcohols by oxidation of hydrocarbons Expired - Lifetime US3683035A (en)

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BE (1) BE715807A (enrdf_load_html_response)
DE (1) DE1768471A1 (enrdf_load_html_response)
FR (1) FR1559604A (enrdf_load_html_response)
GB (1) GB1200553A (enrdf_load_html_response)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3989763A (en) * 1968-04-17 1976-11-02 Nippon Shokubai Kagaku Kogyo Co., Ltd. Method for recovering alcohols

Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2557281A (en) * 1951-06-19 Oxidation op petroleum cyclohexane
US2595786A (en) * 1950-06-01 1952-05-06 Standard Oil Dev Co Treatment of topped oxo alcohol with molecular oxygen and caustic
US2595763A (en) * 1949-12-31 1952-05-06 Standard Oil Dev Co Treatment of oxo alcohols by caustic and air
US2626284A (en) * 1949-09-17 1953-01-20 Standard Oil Dev Co Aqueous caustic treat of iso-octyl alcohol
GB900627A (en) * 1958-02-17 1962-07-11 Bergwerksgesellschaft Hibernia An improved method of producing highly purified ethyl alcohol and an apparatus for carrying out such method
US3232704A (en) * 1962-03-21 1966-02-01 Exxon Research Engineering Co Process for recovering boric acid
US3287423A (en) * 1961-12-21 1966-11-22 Stamicarbon Preparation of cyclic alcohols by oxidation in the presence of boric acid
US3359335A (en) * 1964-05-13 1967-12-19 Exxon Research Engineering Co Caustic scrubbing of aldox alcohols
US3439041A (en) * 1965-01-30 1969-04-15 Vickers Zimmer Ag Oxidation product separation
US3442959A (en) * 1964-08-06 1969-05-06 Halcon International Inc Oxidation of paraffins to provide alcohols

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2557281A (en) * 1951-06-19 Oxidation op petroleum cyclohexane
US2626284A (en) * 1949-09-17 1953-01-20 Standard Oil Dev Co Aqueous caustic treat of iso-octyl alcohol
US2595763A (en) * 1949-12-31 1952-05-06 Standard Oil Dev Co Treatment of oxo alcohols by caustic and air
US2595786A (en) * 1950-06-01 1952-05-06 Standard Oil Dev Co Treatment of topped oxo alcohol with molecular oxygen and caustic
GB900627A (en) * 1958-02-17 1962-07-11 Bergwerksgesellschaft Hibernia An improved method of producing highly purified ethyl alcohol and an apparatus for carrying out such method
US3287423A (en) * 1961-12-21 1966-11-22 Stamicarbon Preparation of cyclic alcohols by oxidation in the presence of boric acid
US3232704A (en) * 1962-03-21 1966-02-01 Exxon Research Engineering Co Process for recovering boric acid
US3359335A (en) * 1964-05-13 1967-12-19 Exxon Research Engineering Co Caustic scrubbing of aldox alcohols
US3442959A (en) * 1964-08-06 1969-05-06 Halcon International Inc Oxidation of paraffins to provide alcohols
US3439041A (en) * 1965-01-30 1969-04-15 Vickers Zimmer Ag Oxidation product separation

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3989763A (en) * 1968-04-17 1976-11-02 Nippon Shokubai Kagaku Kogyo Co., Ltd. Method for recovering alcohols

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FR1559604A (enrdf_load_html_response) 1969-03-14
BE715807A (enrdf_load_html_response) 1968-10-16
GB1200553A (en) 1970-07-29

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