WO2000010947A1 - Procede ameliore de production d'un compose aromatique - Google Patents
Procede ameliore de production d'un compose aromatique Download PDFInfo
- Publication number
- WO2000010947A1 WO2000010947A1 PCT/JP1999/004587 JP9904587W WO0010947A1 WO 2000010947 A1 WO2000010947 A1 WO 2000010947A1 JP 9904587 W JP9904587 W JP 9904587W WO 0010947 A1 WO0010947 A1 WO 0010947A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- reactor
- styrene
- aromatic compound
- reaction mixture
- adduct
- Prior art date
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07B—GENERAL METHODS OF ORGANIC CHEMISTRY; APPARATUS THEREFOR
- C07B61/00—Other general methods
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
- C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
- C07C2/66—Catalytic processes
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
- C07C2521/12—Silica and alumina
Definitions
- the present invention relates to a method for producing an aromatic compound / styrene adduct, for example, a diarylalkane, by reacting an aromatic compound with a styrene using an acid catalyst.
- a method for producing an aromatic compound Z styrene adduct, for example, diaryl alkane by reacting an aromatic compound with styrenes using an acid catalyst is described in US Pat. 44, 279, Japanese Patent Application Laid-Open No. 55-24145, and US Patent Nos. 4,289, 918.
- the obtained aromatic compound / styrene adducts such as diarylalkanes are widely used as various industrial solvents such as insulating oils and solvents for pressure-sensitive paper dyes.
- styrenated xylene in a reaction in which styrene is added to xylene to form styrenated xylene, the double bond of styrene disappears by being added to an aromatic ring, so styrenated xylene itself is usually a saturated compound.
- Unsaturated hydrocarbons such as styrene oligomers such as styrene di- to tetramer are by-produced depending on the catalyst, catalyst, reaction raw material ratio, reaction conditions, etc., and are mixed into styrenated xylene due to their close boiling points. Often enter.
- One of the methods for suppressing the generation of unsaturated hydrocarbons when adding styrenes to aromatic compounds is to reduce the ratio of styrenes to aromatic compounds in the raw material.
- concentration of styrenes in the raw material is reduced, the productivity of the target product is reduced, which is industrially disadvantageous.
- FIG. 1 is a flow sheet showing one embodiment of the method of the present invention. Disclosure of the invention
- a first aspect of the present invention is to add styrenes to an aromatic compound having at least one hydrogen atom directly bonded to an aromatic ring carbon atom by the following steps (1) to (4).
- the present invention relates to a method for producing a compound Z styrene adduct. Step (1): An aromatic compound and styrene are brought into contact with a solid acid catalyst in a liquid phase in a fixed bed flow type first reactor, so that unreacted components, aromatic compound / styrene adduct and non- Obtaining a reaction mixture comprising a saturated component,
- Step (2) circulating a part of the reaction mixture flowing out of the first reactor to the first reactor
- Step (3) supplying the reaction mixture flowing out of the first reactor to the second reactor, and contacting the solid acid catalyst in a liquid phase to reduce the unsaturated components in the reaction mixture;
- Step (4) Addition of aromatic compounds Z styrenes by distilling the reaction mixture A step of obtaining a fraction containing less unsaturated components, mainly composed of the body.
- a second aspect of the present invention relates to the method according to the first aspect, wherein the aromatic compound is benzene or alkylbenzene.
- a third aspect of the present invention relates to the method according to the first aspect, wherein the styrene is styrene or alkylstyrene.
- the aromatic compound as a raw material of the present invention is a compound in which at least one hydrogen atom is bonded to a non-condensed or condensed benzene ring carbon atom.
- alkylbenzenes such as benzene, toluene, xylene, ethylbenzene, cumene, trimethylbenzene, ethylbenzene, getylbenzene, and butylbenzene
- naphthylenes such as naphthalene and methylnaphthalene
- diarylalkanes such as diphenylmethane and diphenylethane
- phenols such as phenol and cresol; and mixtures thereof.
- the styrene used in the present invention is a hydrocarbon compound having at least one conjugated carbon-carbon double bond in a non-condensed or condensed benzene ring, and specifically, styrene and tt-methyl.
- R, and R 9 represent a hydrogen atom or methyl, ethyl, n-propyl And lower alkyl groups such as isopropyl, n-butyl, sec-butyl, tert-butyl and isobutyl, and one Ri and m R 2 may be the same or different.
- R 3 is a divalent hydrocarbon residue from which two hydrogen atoms have been abstracted from benzene or propane. 1 and m are integers from 0 to 5, and n is an integer of 1 or 2.
- phenyl alkane examples include 1, 1-diphenyl, 1-phenyl 2-ethyl-phenyl, 1-phenyl 1-xylylethane, 1-phenyl-1-cumenyletane, 1-phenyl-11-sec-butylphenylethane and the like.
- FIG. 1 is a flow sheet showing one embodiment of the method of the present invention.
- the main part of the reactor shown in the figure is a flow-type first reactor 1 having a fixed bed filled with a solid acid catalyst, and a part of the reaction mixture flowing out from the outlet is returned to the inlet of the first reactor 1 It comprises a line 2 and a second reactor 3 filled with a solid acid catalyst.
- Reference numeral 4 denotes a distillation column in the separation and purification step, and when a reusable raw material remains unreacted, it can be separated and recovered here and reused.
- the aromatic compounds and styrene as raw materials are sent to line 5 by a transfer pump (not shown) in a form preliminarily mixed from a storage tank (not shown), and merged with the circulating flow of circulation line 2. It is supplied to the first reactor 1.
- the aromatic compound and styrenes can be supplied to the first reactor 1 from separate lines as appropriate. Although a reaction solvent can be used, it is usually preferable to carry out the reaction using the aromatic compound itself as a solvent.
- the concentration of the styrene with respect to the total of both components is 0.5 to 70% by weight, preferably 5 to 50% by weight. You can choose from a range. The above total does not include the circulation flow from circulation line 2.
- a flow-type reactor having a fixed bed of a solid acid catalyst is employed.
- a device for heating such as a device for circulating a heat medium, can be provided as appropriate. It may be a single tube system, or may be a multi-tube system as appropriate.
- Cation exchange resins such as cross-linked polystyrene sulfonates (trade name: Amberlyst); synthetic or natural amorphous metal oxides such as clay, silica and alumina Solid acid composed of a substance; zeolite such as Y-type zeolite, ultra-stabilized Y-type zeolite, mordenite, ZSM-5, ZSM-12, and the like.
- the reaction temperature can be selected from the range of 40 to 300 ° C.
- the reaction pressure can be selected such that the reaction phase is in the liquid phase. Usually, for example, it can be selected from the range of 0.01 to 1 OMPa.
- WH SV mass flow rate / catalyst filling mass
- an unsaturated compound is generated together with the aromatic compound / styrene adduct by bringing the aromatic compound and styrene into contact with the solid acid catalyst in a liquid phase.
- 1-phenyl-1-ethylphenylethane with styrene added to ethylbenzene 1-phenyl-1-xylylethane with styrene added to xylene
- sec-butyl Styrene added to benzene 1 1 1 1 see-Butyl phenyl ethane and other unsaturated components are generated.
- These unsaturated components are mainly unsaturated oligomers of styrenes and are composed of di- to tetramers. Since these unsaturated styrene oligomers are close in molecular weight and boiling point to the aromatic compound Z styrene adduct, they are easily mixed into the target aromatic compound / styrene adduct.
- reaction mixture containing an unreacted component composed of an aromatic compound and styrene, an aromatic compound Z-styrene adduct, and an unsaturated component flows out of the outlet of the first reactor.
- a part of the reaction mixture flowing out of the outlet of the first reactor is combined with the raw material of the line 5 by the circulation line 2 and circulated to the first reactor 1 via the line 6.
- the circulation amount is preferably from 1 to 99 parts by weight, more preferably from 25 to 9.9 parts by weight, based on 100 parts by weight of the total outflow of the reaction mixture from the first reactor 1.
- Circulation can be performed by a transfer means (not shown) such as a suitable pump.
- a transfer means such as a suitable pump.
- the remaining reaction mixture circulated as described above is supplied to the second reactor 3 via the line 7 in the figure, where the liquid phase Contact with the solid acid catalyst in
- the effluent from the first reactor 1 may be continuously supplied to the second reactor 3 as shown in the figure, or a storage tank (not shown) for the reaction mixture as appropriate.
- the so-called block operation in which the second reactor is supplied, can be performed.
- the main purpose of providing the second reactor 3 is the following two points. That is,
- the unsaturated component generated in the first reactor 1 specifically, an unsaturated styrene oligomer is alkylated to be converted into an aromatic compound, It undergoes a chemical reaction (cyclization reaction) to convert it into an intramolecular benzene ring.
- cyclization reaction a chemical reaction to convert it into an intramolecular benzene ring.
- unsaturated styrene oligomers are converted to saturated compounds without unsaturated carbon-carbon double bonds.
- the same catalyst as the solid acid catalyst used in the first reactor 1 can be used.
- Solid catalysts that are substantially less shape-selective than zeolites having the function of so-called molecular sieves such as solid acid catalysts composed of synthetic or natural amorphous metal oxides represented by clay and silica-alumina, and cross-linking
- a cation exchange resin represented by a sulfonated product of polystyrene (trade name: Amberlyst) is preferred, and a solid acid catalyst comprising an amorphous metal oxide is particularly preferred.
- the reaction type of the second reactor 3 may be a continuous type or a batch type, and any of a stirred tank type and a fixed bed flow type may be used. Preferably, it is a fixed bed flow type similar to the first reactor.
- the reaction conditions can be in the same range as in the case of the first reactor.
- the reaction temperature can be selected from the range of 40 to 300 ° C.
- the reaction pressure can be selected so that the reaction phase is a liquid phase, and usually can be selected, for example, from the range of 0.01 to 10 MPa.
- the WH SV when the fixed bed flow type is adopted can be selected from the range of 0.1 to 200 h 1 based on the flow rate of the raw material passing through the line 5.
- the figure shows a case where a fixed bed flow type is adopted as the second reactor 3.
- the effluent leaving the second reactor 3 enters the distillation column 4 via the line 8, and after performing distillation, the fraction containing the aromatic compound Z styrene adduct as the target substance is obtained from the line 9. Is taken out.
- a fraction containing an aromatic compound Z styrene adduct such as di-alkyl alkane having a small amount of unsaturated components can be easily obtained by distillation or the like, which is an industrial separation means.
- distillation column 4 Ordinary industrial distillation conditions can be employed.Specifically, a packed column packed with appropriate packing is used, for example, the number of separation stages is 2 to 200, the reflux ratio is 0.1 to 50, and the pressure is It can be performed in the range of 100 Pa to 100 kPa.
- the aromatic compound supplied in excess and the unreacted styrene and the like, if necessary, are separated and collected, and are appropriately combined with the line 5 via the storage tank (not shown) via the line 10; It can be circulated from line 6 to the first reactor 1. Further, in order to recover such unreacted components, the distillation column 4 can be appropriately formed into a series or parallel multi-stage distillation column.
- the fraction containing the aromatic compound Z-styrene adduct taken out from line 9 has few unsaturated components, so that thermal stability and oxidation stability are rarely reduced. It is useful as various industrial hydrocarbon solvents such as insulating oils and solvents for pressure-sensitive paper dyes.
- reactor 1 was filled with 2 g of silica / alumina (trade name: IS-28, manufactured by Mizusawa Chemical Industry Co., Ltd.), and the molar ratio of cumene to styrene was The raw materials mixed in a ratio of 10: 1 were supplied at a flow rate of 2 Og / h, and the operation was continuously performed with a circulation rate of 40 Og / h. went.
- silica / alumina trade name: IS-28, manufactured by Mizusawa Chemical Industry Co., Ltd.
- a reaction mixture containing 1-phenyl-2-cumeneylethane and unsaturated styrene oligomer flowing out from the outlet of the first reactor was withdrawn at a flow rate of 2 Og / h, and once stored in a storage tank (not shown).
- the reaction solution in this storage tank was analyzed by gas chromatography, and the content of 11-phenyl-2-cumenylethane and styrene dimer in the reaction product was estimated from the results.
- the bromine value of the reaction product obtained by removing unreacted components from the same reaction solution was measured as an index of the amount of the compound having an unsaturated double bond. Table 1 shows the results.
- reaction mixture was withdrawn at a flow rate of 1 Og / h from the above storage tank, and this was mixed with silica-alumina (trade name: N632L, manufactured by Nikki Chemical Co., Ltd.).
- silica-alumina trade name: N632L, manufactured by Nikki Chemical Co., Ltd.
- the mixture was supplied to the second reactor 3 as a vessel, and further reacted at a temperature of 150 ° C. and a pressure of 0.5 MPa.
- the operation of the first reactor was performed in the same manner as in the example, except that the circulation line 2 in the first reactor 1 was cut off and the circulation was not performed. That is, a raw material obtained by charging 2 g of silica 'alumina (trade name: IS-28, manufactured by Mizusawa Chemical Industry Co., Ltd.) in the first reactor and mixing cumene and styrene in a molar ratio of 10: 1. Operation at a flow rate of 20 g / h The reaction was carried out at a temperature of 150 ° C. and a pressure of 1 MPa.
- the method of the present invention it is possible to supply a higher concentration of styrene to the reaction system than in the conventional method, and as a result, it is possible to reduce the size of the apparatus when compared at the same production volume. It is also possible to reduce the operating costs of the device.
- an aromatic compound / styrene adduct such as a dialkyl alkane having a low unsaturation component, that is, a low bromine value is easily contained by distillation or the like which is an industrial separation means. A fraction can be obtained in high yield.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP99940479A EP1026136B1 (en) | 1998-08-25 | 1999-08-25 | Improved method for producing aromatic compound |
JP2000566223A JP4336045B2 (ja) | 1998-08-25 | 1999-08-25 | 改良された芳香族化合物の製造方法 |
US09/529,750 US6350930B1 (en) | 1998-08-25 | 1999-08-25 | Method for producing aromatic compound |
DE69908544T DE69908544T2 (de) | 1998-08-25 | 1999-08-25 | Verbessertes verfahren zur herstellung aromatischer verbindungen |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP25461298 | 1998-08-25 | ||
JP10/254612 | 1998-08-25 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2000010947A1 true WO2000010947A1 (fr) | 2000-03-02 |
Family
ID=17267463
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP1999/004587 WO2000010947A1 (fr) | 1998-08-25 | 1999-08-25 | Procede ameliore de production d'un compose aromatique |
Country Status (5)
Country | Link |
---|---|
US (1) | US6350930B1 (ja) |
EP (1) | EP1026136B1 (ja) |
JP (1) | JP4336045B2 (ja) |
DE (1) | DE69908544T2 (ja) |
WO (1) | WO2000010947A1 (ja) |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS53135959A (en) * | 1977-04-27 | 1978-11-28 | Nippon Petrochemicals Co Ltd | Aralkylation of alkylbenzen |
JPS6242938A (ja) * | 1985-08-20 | 1987-02-24 | Kawasaki Steel Corp | 高沸点炭化水素油の製造法 |
JPH04257530A (ja) * | 1991-02-08 | 1992-09-11 | Idemitsu Petrochem Co Ltd | アラルキルベンゼン類の製造方法 |
JPH09104645A (ja) * | 1995-07-14 | 1997-04-22 | Basf Ag | ジアリールエタンの製法 |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS54154742A (en) * | 1978-05-24 | 1979-12-06 | Kureha Chem Ind Co Ltd | Preparation of diarylethane derivative |
JPS5524145A (en) | 1978-08-10 | 1980-02-21 | Nippon Petrochem Co Ltd | Preparation of non-condensed bicyclic aromatic compound |
US4220557A (en) * | 1978-11-24 | 1980-09-02 | Union Oil Company Of California | Fluorine-promoted sulfactive metal hydrogenation catalysts |
JPS5618928A (en) | 1979-07-24 | 1981-02-23 | Nippon Petrochem Co Ltd | Aralkylation of alkylbenzene |
JPS60208398A (ja) | 1984-03-31 | 1985-10-19 | Nippon Petrochem Co Ltd | 機能性流体の製造法 |
-
1999
- 1999-08-25 EP EP99940479A patent/EP1026136B1/en not_active Expired - Lifetime
- 1999-08-25 JP JP2000566223A patent/JP4336045B2/ja not_active Expired - Lifetime
- 1999-08-25 US US09/529,750 patent/US6350930B1/en not_active Expired - Lifetime
- 1999-08-25 WO PCT/JP1999/004587 patent/WO2000010947A1/ja active IP Right Grant
- 1999-08-25 DE DE69908544T patent/DE69908544T2/de not_active Expired - Lifetime
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS53135959A (en) * | 1977-04-27 | 1978-11-28 | Nippon Petrochemicals Co Ltd | Aralkylation of alkylbenzen |
JPS6242938A (ja) * | 1985-08-20 | 1987-02-24 | Kawasaki Steel Corp | 高沸点炭化水素油の製造法 |
JPH04257530A (ja) * | 1991-02-08 | 1992-09-11 | Idemitsu Petrochem Co Ltd | アラルキルベンゼン類の製造方法 |
JPH09104645A (ja) * | 1995-07-14 | 1997-04-22 | Basf Ag | ジアリールエタンの製法 |
Non-Patent Citations (1)
Title |
---|
See also references of EP1026136A4 * |
Also Published As
Publication number | Publication date |
---|---|
US6350930B1 (en) | 2002-02-26 |
EP1026136B1 (en) | 2003-06-04 |
DE69908544T2 (de) | 2004-05-06 |
JP4336045B2 (ja) | 2009-09-30 |
EP1026136A1 (en) | 2000-08-09 |
DE69908544D1 (de) | 2003-07-10 |
EP1026136A4 (en) | 2001-07-04 |
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