EP2303822A1 - Verfahren zur herstellung von cyclohexanon - Google Patents

Verfahren zur herstellung von cyclohexanon

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Publication number
EP2303822A1
EP2303822A1 EP09739316A EP09739316A EP2303822A1 EP 2303822 A1 EP2303822 A1 EP 2303822A1 EP 09739316 A EP09739316 A EP 09739316A EP 09739316 A EP09739316 A EP 09739316A EP 2303822 A1 EP2303822 A1 EP 2303822A1
Authority
EP
European Patent Office
Prior art keywords
cyclohexanone
effluent stream
phenol
cyclohexylbenzene
effluent
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP09739316A
Other languages
English (en)
French (fr)
Inventor
Jihad M. Dakka
John Scott Buchanan
James R. Lattner
Sadi Mizrahi
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ExxonMobil Chemical Patents Inc
Original Assignee
ExxonMobil Chemical Patents Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by ExxonMobil Chemical Patents Inc filed Critical ExxonMobil Chemical Patents Inc
Priority to EP09739316A priority Critical patent/EP2303822A1/de
Publication of EP2303822A1 publication Critical patent/EP2303822A1/de
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C409/00—Peroxy compounds
    • C07C409/02—Peroxy compounds the —O—O— group being bound between a carbon atom, not further substituted by oxygen atoms, and hydrogen, i.e. hydroperoxides
    • C07C409/14—Peroxy compounds the —O—O— group being bound between a carbon atom, not further substituted by oxygen atoms, and hydrogen, i.e. hydroperoxides the carbon atom belonging to a ring other than a six-membered aromatic ring
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
    • C07C37/06—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by conversion of non-aromatic six-membered rings or of such rings formed in situ into aromatic six-membered rings, e.g. by dehydrogenation
    • C07C37/07—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by conversion of non-aromatic six-membered rings or of such rings formed in situ into aromatic six-membered rings, e.g. by dehydrogenation with simultaneous reduction of C=O group in that ring
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
    • C07C37/08—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by decomposition of hydroperoxides, e.g. cumene hydroperoxide
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C407/00—Preparation of peroxy compounds
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/006—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by hydrogenation of aromatic hydroxy compounds
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/51—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by pyrolysis, rearrangement or decomposition
    • C07C45/53—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by pyrolysis, rearrangement or decomposition of hydroperoxides
    • 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

  • the present invention relates to a process for producing cyclohexanone.
  • Cyclohexanone is an important product in the chemical industry and is useful as, for example, an industrial solvent, as an activator in oxidation reactions and in the production of adipic acid, cyclohexanone resins, cyclohexanone oxime, caprolactam and nylon 6.
  • the most common route for the production of cyclohexanone is by oxidation of cyclohexane to cyclohexyl hydroperoxide, which is then cleaved to produce cyclohexanol and cyclohexanone in substantially equimolar amounts.
  • Another potential route for the production of cyclohexanone is by a variation of the Hock process, in which benzene is converted to cyclohexylbenzene and the cyclohexylbenzene is oxidized to produce cyclohexylbenzene hydroperoxide, which is then cleaved to produce cyclohexanone and phenol in substantially equimolar amounts.
  • This route has the potential advantage that phenol is a highly valued intermediate in the production of phenolic resins, bisphenol A, ⁇ -caprolactam, adipic acid, and plasticizers.
  • the present invention seeks to address these problems by providing a process for producing cyclohexanone by oxidation of cyclohexylbenzene to cyclohexylbenzene hydroperoxide followed by cleavage of the cyclohexylbenzene hydroperoxide, in which at least a portion of the effluent from the cleavage step is subjected to a selective hydrogenation step.
  • the hydrogenation step converts at least part of the phenol in the effluent portion to additional cyclohexanone.
  • the cleavage effluent portion subjected to the hydrogenation step can be a substantially pure phenol fraction separated from the raw effluent, given the cost of this separation, the process can also be applied to an effluent portion containing some or all of the cyclohexanone produced in the cleavage step. In this way, the total cost of purifying the final cyclohexanone stream and, if present, the final phenol stream can be minimized. Then, depending on the then current demand for phenol, part or all of the cyclohexanone could be dehydrogenated back to phenol. Alternatively, all the cyclohexanone could be recovered as saleable product.
  • the invention resides in a process for producing cyclohexanone, the process comprising: (a) oxidizing cyclohexylbenzene to produce cyclohexylbenzene hydroperoxide;
  • said effluent stream portion fed to said hydrogenation reaction zone has the same composition as the effluent stream produced by said converting (b).
  • the process further includes subjecting the effluent stream produced by said converting (b) to at least one separation step such that said effluent stream portion fed to said dehydrogenation reaction zone contains less cyclohexanone than the effluent stream producing by said converting (b).
  • the conditions in (d) comprise a temperature of about 20 0 C to about 250 0 C and/or a pressure of about 101 kPa to about 10,000 kPa and/or a hydrogen to phenol molar ratio of about 1 :1 to about 100:1.
  • the hydrogenation catalyst comprises platinum and/or palladium.
  • the invention resides in a process for producing cyclohexanone, the process comprising:
  • step (2) corresponds to previously stated process steps (a), (b), (c) and (d), respectively.
  • step (1) may be considered as an optional cyclohexylbenzene feedstock-producing step that, in a preferred embodiment, precedes step (a).
  • the process of the invention comprises a preliminary step of contacting benzene and hydrogen with a catalyst under hydroalkylation conditions to produce the cyclohexylbenzene for oxidizing in step (a).
  • cyclohexylbenzene which in a preferred embodiment is produced by the catalytic hydroalkylation of benzene, is oxidized to produce cyclohexylbenzene hydroperoxide and then the cyclohexylbenzene hydroperoxide is cleaved to produce an effluent stream comprising phenol and cyclohexanone in substantially equimolar amounts.
  • At least a portion of the effluent stream is then fed to a hydrogenation reaction zone, where the effluent stream portion is contacted with hydrogen in the presence of a hydrogenation catalyst and under conditions effective to convert the cyclohexanone in said effluent portion into additional phenol.
  • the cyclohexylbenzene employed in the present process can be produced by any conventional technique, including alkylation of benzene with cyclohexene in the presence of an acid catalyst, such as zeolite beta or an MCM-22 family molecular sieve, or by oxidative coupling of benzene to biphenyl followed by hydrogenation of the biphenyl.
  • an acid catalyst such as zeolite beta or an MCM-22 family molecular sieve
  • oxidative coupling of benzene to biphenyl followed by hydrogenation of the biphenyl is generally produced by contacting benzene with hydrogen under hydroalkylation conditions in the presence of a hydroalkylation catalyst whereby the benzene undergoes the following reaction (I) to produce cyclohexylbenzene (CHB):
  • any commercially available benzene feed can be used in the hydroalkylation step, but preferably the benzene has a purity level of at least 99 wt%.
  • the source of hydrogen is not critical, it is generally desirable that the hydrogen is at least 99 wt% pure.
  • the total feed to the hydroalkylation step contains less than 1000 ppm, such as less than 500 ppm, for example less than 100 ppm by weight, water and/or less than 100 ppm, such as less than 30 ppm, for example less than 3 ppm by weight, sulfur and/or less than 10 ppm, such as less than 1 ppm, for example less than 0.1 ppm by weight, nitrogen.
  • the hydroalkylation reaction can be conducted in a wide range of reactor configurations including fixed bed, slurry reactors, and/or catalytic distillation towers.
  • the hydroalkylation reaction can be conducted in a single reaction zone or in a plurality of reaction zones, in which at least the hydrogen is introduced to the reaction in stages.
  • Suitable reaction temperatures are between about 100 0 C and about 400 0 C, such as between about 125°C and about 25O 0 C.
  • Suitable reaction pressures are between about 100 and about 7,000 kPa, such as between about 500 and about 5,000 kPa.
  • Suitable values for the molar ratio of hydrogen to benzene are between about 0.15:1 and about 15:1, such as between about 0.4: 1 and about 4:1 for example between about 0.4 and about 0.9: 1.
  • the catalyst employed in the hydroalkylation reaction is preferably a bifunctional catalyst comprising a molecular sieve of the MCM-22 family and a hydrogenation metal.
  • MCM-22 family material or “material of the MCM-22 family” or “molecular sieve of the MCM-22 family”, as used herein, includes one or more of:
  • molecular sieves made from a common first degree crystalline building block unit cell which unit cell has the MWW framework topology.
  • a unit cell is a spatial arrangement of atoms which if tiled in three-dimensional space describes the crystal structure. Such crystal structures are discussed in the "Atlas of Zeolite Framework Types", Fifth edition, 2001, the entire content of which is incorporated as reference);
  • molecular sieves made from a common second degree building block being a 2- dimensional tiling of such MWW framework topology unit cells, forming a monolayer of one unit cell thickness, preferably one c-unit cell thickness;
  • molecular sieves made from common second degree building blocks, being layers of one or more than one unit cell thickness, wherein the layer of more than one unit cell thickness is made from stacking, packing, or binding at least two monolayers of one unit cell thickness.
  • the stacking of such second degree building blocks can be in a regular fashion, an irregular fashion, a random fashion, or any combination thereof;
  • molecular sieves made by any regular or random 2-dimensional or 3 -dimensional combination of unit cells having the MWW framework topology.
  • Molecular sieves of MCM-22 family generally have an X-ray diffraction pattern including d-spacing maxima at 12.4 ⁇ 0.25, 6.9 ⁇ 0.15, 3.57 ⁇ 0.07 and 3.42 ⁇ 0.07 Angstrom.
  • the X-ray diffraction data used to characterize the material are obtained by standard techniques such as using the K-alpha doublet of copper as the incident radiation and a diffractometer equipped with a scintillation counter and associated computer as the collection system.
  • Molecular sieves of MCM-22 family include MCM-22 (described in U.S. Patent No. 4,954,325), PSH-3 (described in U.S. Patent No. 4,439,409), SSZ-25 (described in U.S. Patent No.
  • the molecular sieve is selected from (a) MCM-49, (b) MCM-56 and (c) isotypes of MCM-49 and MCM-56, such as ITQ-2.
  • any known hydrogenation metal can be employed in the hydroalkylation catalyst although suitable metals include palladium, ruthenium, nickel, zinc, tin and cobalt, with palladium being particularly advantageous.
  • the amount of hydrogenation metal present in the catalyst is between about 0.05 and about 10 wt %, such as between about 0.1 and about 5 wt %, of the catalyst.
  • the amount of hydrogenation metal present is such that the molar ratio of the aluminum in the molecular sieve to the hydrogenation metal is from about 1.5 to about 1500, for example from about 75 to about 750, such as from about 100 to about 300.
  • the hydrogenation metal may be directly supported on the MCM-22 family molecular sieve by, for example, impregnation or ion exchange.
  • at least 50 wt%, for example at least 75wt%, and particularly preferably substantially all (eg at least 95, 98 or 99 wt%) or even 100 wt% of the hydrogenation metal is supported on an inorganic oxide separate from but composited with the molecular sieve.
  • the activity of the catalyst and its selectivity to cyclohexylbenzene and dicyclohexylbenzene are increased as compared with an equivalent catalyst in which the hydrogenation metal is supported on the molecular sieve.
  • the inorganic oxide employed in such a composite hydroalkylation catalyst is not narrowly defined provided it is stable and inert under the conditions of the hydroalkylation reaction. Suitable inorganic oxides include oxides of Groups 2, 4, 13 and 14 of the Periodic Table of Elements, such as alumina and/or titania and/or zirconia. As used herein, the numbering scheme for the Periodic Table Groups is as disclosed in Chemical and Engineering News, 63(5), 27 (1985).
  • the hydrogenation metal is conveniently deposited on the inorganic oxide, conveniently by impregnation, before the metal-containing inorganic oxide is composited with the molecular sieve.
  • the catalyst composite is produced by co-pelletization, in which a mixture of the molecular sieve and the metal-containing inorganic oxide are formed into pellets at high pressure (generally about 350 to about 350,000 kPa), or by co- extrusion, in which a slurry of the molecular sieve and the metal-containing inorganic oxide, optionally together with a separate binder, are forced through a die. If necessary, additional hydrogenation metal can subsequently be deposited on the resultant catalyst composite.
  • the catalyst may also comprise a binder.
  • the binder materials include synthetic or naturally occurring substances as well as inorganic materials such as clay, silica and/or metal oxides.
  • the latter may be either naturally occurring or in the form of gelatinous precipitates or gels including mixtures of silica and metal oxides.
  • Naturally occurring clays which can be used as a binder include those of the montmorillonite and kaolin families, which families include the subbentonites and the kaolins commonly known as Dixie, McNamee, Georgia and Florida clays or others in which the main mineral constituent is halloysite, kaolinite, dickite, nacrite or anauxite. Such clays can be used in the raw state as originally mined or initially subjected to calcination, acid treatment or chemical modification.
  • Suitable metal oxide binders include silica, alumina, zirconia, titania, silica- alumina, silica-magnesia, silica-zirconia, silica-thoria, silica-beryllia and silica-titania as well as ternary compositions such as silica-alumina-thoria, silica-alumina-zirconia, silica-alumina- magnesia and silica-magnesia-zirconia.
  • the hydroalkylation step is highly selective towards cyclohexylbenzene
  • the effluent from the hydroalkylation reaction will normally contain some dialkylated products, as well as unreacted aromatic feed and the desired monoalkylated species.
  • the unreacted aromatic feed is normally recovered by distillation and recycled to the alkylation reactor.
  • the bottoms from the benzene distillation are further distilled to separate the monocyclohexylbenzene product from any dicyclohexylbenzene and other heavies.
  • Transalkylation with additional benzene is typically effected in a transalkylation reactor, separate from the hydroalkylation reactor, over a suitable transalkylation catalyst, such as a molecular sieve of the MCM-22 family, zeolite beta, MCM-68 (see U.S. Patent No. 6,014,018), zeolite Y or mordenite.
  • a transalkylation catalyst such as a molecular sieve of the MCM-22 family, zeolite beta, MCM-68 (see U.S. Patent No. 6,014,018), zeolite Y or mordenite.
  • the transalkylation reaction is typically conducted under at least partial liquid phase conditions, which suitably include a temperature of about 100 to about 300 0 C, a pressure of about 800 to about 3500 kPa, a weight hourly space velocity of about 1 to about 10 hr "1 on total feed, and a benzene/dicyclohexylbenzene weight ratio about of 1 :1 to about 5:1.
  • a temperature of about 100 to about 300 0 C a pressure of about 800 to about 3500 kPa
  • a weight hourly space velocity of about 1 to about 10 hr "1 on total feed
  • benzene/dicyclohexylbenzene weight ratio about of 1 :1 to about 5:1.
  • the cyclohexylbenzene is initially oxidized to the corresponding hydroperoxide. This may be accomplished by introducing an oxygen-containing gas, such as air, into a liquid phase containing the cyclohexylbenzene.
  • an oxygen-containing gas such as air
  • atmospheric air oxidation of cyclohexylbenzene in the absence of a catalyst is very slow and hence the oxidation is normally conducted in the presence of a catalyst.
  • Suitable catalysts for the cyclohexylbenzene oxidation step are the N-hydroxy substituted cyclic imides described in U.S. Patent No. 6,720,462 and incorporated herein by reference, such as N-hydroxyphthalimide, 4-amino-N-hydroxyphthalimide, 3-amino-N- hydroxyphthalimide, tetrabromo-N-hydroxyphthalimide, tetrachloro-N-hydroxyphthalimide, N-hydroxyhetimide, N-hydroxyhimimide, N-hydroxytrimellitimide, N-hydroxybenzene- 1,2,4-tricarboximide, N,N'-dihydroxy(pyromellitic diimide), N,N'-dihydroxy(benzophenone- 3,3',4,4'-tetracarboxylic diimide), N-hydroxymaleimide, pyridine-2,3-dicarboximide, N- hydroxysuccinimide, N-hydroxy(tartaric imide), N-
  • the catalyst is N-hydroxyphthalimide.
  • Another suitable catalyst is N,N',N"-trihydroxyisocyanuric acid.
  • These catalytic materials can be used either alone or in the presence of a free radical initiator and can be used as liquid-phase, homogeneous catalysts or can be supported on a solid carrier to provide a heterogeneous catalyst.
  • the N-hydroxy substituted cyclic imide or the N,N',N"-trihydroxyisocyanuric acid is employed in an amount of from 0.0001 mol % to 15 mol %, such as from 0.001 to 5 mol %, of the cyclohexylbenzene.
  • Suitable conditions for the oxidation step include a temperature between about 70 0 C and about 200 0 C, such as about 90 0 C to about 130 0 C, and/or a pressure of about 50 to 10,000 kPa.
  • Any oxygen-containing gas preferably air, can be used as the oxidizing medium.
  • the reaction can take place in batch reactors or continuous flow reactors.
  • a basic buffering agent may be added to react with acidic by-products that may form during the oxidation.
  • an aqueous phase may be introduced, which can help dissolve basic compounds, such as sodium carbonate. Hydroperoxide Cleavage
  • the final reactive step in the conversion of the cyclohexylbenzene into phenol and cyclohexanone involves cleavage of the cyclohexylbenzene hydroperoxide, which is conveniently effected by contacting the hydroperoxide with a catalyst in the liquid phase at a temperature of for example about 20 0 C to about 15O 0 C, such as about 40 0 C to about 12O 0 C, and/or a pressure of about 50 to about 2,500 kPa, such as about 100 to about 1000 kPa.
  • the cyclohexylbenzene hydroperoxide is preferably diluted in an organic solvent inert to the cleavage reaction, such as methyl ethyl ketone, cyclohexanone, phenol or cyclohexylbenzene, to assist in heat removal.
  • the cleavage reaction is conveniently conducted in a catalytic distillation unit.
  • the catalyst employed in the cleavage step can be a homogeneous catalyst or a heterogeneous catalyst.
  • Suitable homogeneous cleavage catalysts include sulfuric acid, perchloric acid, phosphoric acid, hydrochloric acid and p-toluenesulfonic acid. Ferric chloride, boron trifluoride, sulfur dioxide and sulfur trioxide are also effective homogeneous cleavage catalysts.
  • the preferred homogeneous cleavage catalyst is sulfuric acid, with preferred concentrations in the range of 0.05 to 0.5 wt%.
  • a neutralization step preferably follows the cleavage step. Such a neutralization step typically involves contact with a basic component, with subsequent decanting of a salt-enriched aqueous phase.
  • a suitable heterogeneous catalyst for use in the cleavage of cyclohexylbenzene hydroperoxide includes a smectite clay, such as an acidic montmorillonite silica-alumina clay, as described in U.S. Patent No. 4,870,217, the entire disclosure of which is incorporated herein by reference.
  • Post Treatment of Cleavage Effluent [0037] The effluent from the cleavage reaction comprises phenol and cyclohexanone in substantially equimolar amounts.
  • the present process provides an advantageous route to increasing the amount of cyclohexanone produced from the original benzene feed by contacting at least part of the cleavage effluent with hydrogen in the presence of a hydrogenation catalyst so as to convert some or all of the phenol in the effluent into additional cyclohexanone according to the reaction (II):
  • Any suitable hydrogenation catalyst can be used in reaction (II), such as, for example, a platinum or palladium catalyst.
  • the hydrogenation conditions do not have to be closely controlled. They typically comprise a temperature of about 20 0 C to about 250 0 C and/or a pressure of about 101 kPa to about 10,000 kPa and/or a hydrogen to phenol molar ratio of about 1 :1 to about 100:1.
  • the hydrogenation reaction can be conducted in a wide range of reactor configurations including fixed bed, slurry reactors, and/or catalytic distillation towers.
  • an activated palladium catalyst such as that described in U.S. Patent No. 5,395,076, is employed.
  • the conditions for the hydrogenation step comprise a temperature of about 150 0 C to about 250 0 C and/or a pressure of about 0.8 to about 8 bar (80 kPa to 800 kPa), and/or a hydrogen to phenol molar ratio of about 3.5:1 to about 10:1.
  • the catalyst is preferably activated with hydrogen-containing gases, in particular hydrogen/nitrogen mixtures, or with pure hydrogen.
  • Such activation may be, for example for about 50 hours to about 10 hours at for example about 300 0 C to about 500 0 C, preferably for 40 hours to 20 hours at for example about 350 0 C to about 450 0 C, more preferably for about 35 to about 20 hours at for example about 370 0 C to about 450 0 C. It has been found that by employing such activation, the hydrogenation may proceed with high selectivity to cyclohexanone , such that the molar ratio of cyclohexanone to cyclohexanol in the product is for example between 85:15 and 98:2.
  • cyclohexanone and phenol produce an azeotropic mixture composed of 28 wt% cyclohexanone and 72 wt% phenol, so that any attempt to separate the effluent from the cyclohexylbenzene hydroperoxide cleavage step by simple distillation results in this azeotropic mixture.
  • the efficiency of the separation can be enhanced by conducting the distillation under at least partial vacuum, typically at below 101 kPa.
  • extractive distillation processes are known for separating cyclohexanone and phenol, see for example, U.S. Patent Nos.
  • the feed to the hydrogenation step has the same composition as the cleavage effluent, thereby avoiding the need for an initial expensive separation step.
  • the final product may be substantially free of phenol, thereby at least reducing the problem of separating the phenol from the cyclohexanone in the cleavage effluent.
  • the cleavage effluent is subjected to one or more separation processes to recover or remove one or more components of the effluent prior to hydrogenation.
  • the cleavage effluent is conveniently subjected to at least a first separation step to recover some or all of the cyclohexanone from the effluent, typically so that the effluent stream fed to the hydrogenation reaction contains less than 50 wt%, for example less than 30 wt%, such as from 0.5 to 20 wt%, and particularly less than 1 wt%, cyclohexanone.
  • the first separation step is conveniently effected by vacuum distillation and the same, or additional vacuum distillation steps, can be used to remove components boiling below 155°C (as measured at 101 kPa), such as benzene and cyclohexene, and/or components boiling above 185°C (as measured at 101 kPa), such as 2-phenyl phenol and diphenyl ether, prior to feeding the effluent stream to the hydrogenation reaction.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
EP09739316A 2008-05-01 2009-02-19 Verfahren zur herstellung von cyclohexanon Withdrawn EP2303822A1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP09739316A EP2303822A1 (de) 2008-05-01 2009-02-19 Verfahren zur herstellung von cyclohexanon

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US4954008P 2008-05-01 2008-05-01
EP08158572 2008-06-19
PCT/US2009/034514 WO2009134514A1 (en) 2008-05-01 2009-02-19 Process for producing cyclohexanone
EP09739316A EP2303822A1 (de) 2008-05-01 2009-02-19 Verfahren zur herstellung von cyclohexanon

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EP2303822A1 true EP2303822A1 (de) 2011-04-06

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EP (1) EP2303822A1 (de)
CN (2) CN105198715A (de)
WO (1) WO2009134514A1 (de)

Families Citing this family (28)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20130081294A (ko) 2008-08-29 2013-07-16 엑손모빌 케미칼 패턴츠 인코포레이티드 페놀 제조 방법
CN106824186A (zh) 2010-02-05 2017-06-13 埃克森美孚化学专利公司 环己酮脱氢催化剂和方法
WO2011096990A2 (en) 2010-02-05 2011-08-11 Exxonmobil Chemical Patents Inc. Dehydrogenation catalyst and process
US9029611B2 (en) 2010-02-05 2015-05-12 Exxonmobil Chemical Patents Inc. Dehydrogenation of cyclohexanone to produce phenol
WO2011096993A2 (en) * 2010-02-05 2011-08-11 Exxonmobil Chemical Patents Inc. Dehydrogenation process
CN102958886B (zh) 2010-06-25 2015-07-22 埃克森美孚化学专利公司 脱氢方法
EP2616426A1 (de) * 2010-09-14 2013-07-24 ExxonMobil Chemical Patents Inc. Cyclohexanonzusammensetzungen
CN103097351B (zh) * 2010-09-14 2016-03-09 埃克森美孚化学专利公司 环己基苯的氧化方法
WO2012118542A1 (en) * 2011-02-28 2012-09-07 Exxonmobil Chemical Patents Inc. Process for producing phenol
CN104066704B (zh) * 2011-10-17 2016-05-25 埃克森美孚化学专利公司 生产环己基苯的方法
US8981158B2 (en) 2011-12-19 2015-03-17 Exxonmobil Chemical Patents Inc. Oxidation of cyclohexylbenzene
US9458067B2 (en) * 2012-02-08 2016-10-04 Exxonmobil Chemical Patents Inc. Process for producing cyclohexylbenzene
KR20170027855A (ko) * 2014-08-15 2017-03-10 엑손모빌 케미칼 패턴츠 인코포레이티드 사이클로헥사논의 제조를 위한 방법 및 시스템
EP3180304B1 (de) 2014-08-15 2019-10-30 ExxonMobil Chemical Patents Inc. Verfahren zur herstellung von cyclohexanon
US9926254B2 (en) 2014-08-15 2018-03-27 Exxonmobil Chemical Patents Inc. Process and system for making cyclohexanone
WO2016025218A1 (en) * 2014-08-15 2016-02-18 Exxonmobil Chemical Patents Inc. Process and system for making cyclohexanone
WO2016053466A1 (en) 2014-09-30 2016-04-07 Exxonmobil Chemical Patents Inc. Process for making cyclohexanone
SG11201701429SA (en) * 2014-09-30 2017-04-27 Exxonmobil Chemical Patents Inc Process for making cyclohexanone
SG11201701945RA (en) * 2014-09-30 2017-04-27 Exxonmobil Chemical Patents Inc Process for making cyclohexanone
US20180186715A1 (en) 2015-07-29 2018-07-05 Exxonmobil Chemical Patents Inc. Cyclohexanone Compositions and Processes for Making Such Compositions
WO2017023430A1 (en) * 2015-07-31 2017-02-09 Exxonmobil Chemical Patents Inc. Process for making cyclohexanone
US10252968B2 (en) 2015-07-31 2019-04-09 Exxonmobil Chemical Patents Inc. Process for making cyclohexanone
CN106631954B (zh) * 2015-10-30 2019-05-21 中国石油化工股份有限公司 环己基苯催化氧化生产环己基苯过氧化氢以及环己基苯氧化分解制备环己酮和苯酚的方法
TWI646076B (zh) * 2016-09-09 2019-01-01 中國石油化學工業開發股份有限公司 酚氫化反應生成環己酮之方法
WO2019005274A1 (en) 2017-06-28 2019-01-03 Exxonmobil Chemical Patents Inc. PROCESS FOR PRODUCTION OF CYCLOHEXANONE
WO2019005276A1 (en) 2017-06-28 2019-01-03 Exxonmobil Chemical Patents Inc. PRODUCTS CONTAINING CYCLOHEXANONE AND METHODS OF MAKING THE SAME
WO2019005273A1 (en) 2017-06-28 2019-01-03 Exxonmobil Chemical Patents Inc. PRODUCTS CONTAINING CYCLOHEXANONE AND METHODS OF MAKING THE SAME
CN109999896B (zh) * 2019-04-19 2020-09-25 大连理工大学 一种应用于苯酚选择性加氢制环己酮高效催化剂及其制备方法

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3076810A (en) * 1960-06-15 1963-02-05 Allied Chem Process for the production of cyclohexanone
BE605656A (fr) * 1960-07-06 1961-11-03 Scient Design Co Procédé de préparation du phénol
US4162267A (en) * 1978-06-22 1979-07-24 Allied Chemical Corporation Production of cyclohexanone
US4167456A (en) * 1978-10-06 1979-09-11 Phillips Petroleum Co. Extractive distillation to separate cyclohexylbenzene from phenol-cyclohexanone mixture containing the same
US4328372A (en) * 1979-06-27 1982-05-04 Phillips Petroleum Company Recovery of cyclohexanone from cyclohexylbenzene hydroperoxide acid cleavage product
US4520129A (en) * 1981-08-17 1985-05-28 Phillips Petroleum Compagny Hydrogenation catalyst
US6037513A (en) * 1998-07-09 2000-03-14 Mobil Oil Corporation Hydroalkylation of aromatic hydrocarbons

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2009134514A1 *

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