CN114057549B - Method for simultaneously preparing phenol and benzenediol - Google Patents

Method for simultaneously preparing phenol and benzenediol Download PDF

Info

Publication number
CN114057549B
CN114057549B CN202010747645.7A CN202010747645A CN114057549B CN 114057549 B CN114057549 B CN 114057549B CN 202010747645 A CN202010747645 A CN 202010747645A CN 114057549 B CN114057549 B CN 114057549B
Authority
CN
China
Prior art keywords
molecular sieve
zirconium
benzene
molar ratio
reaction
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.)
Active
Application number
CN202010747645.7A
Other languages
Chinese (zh)
Other versions
CN114057549A (en
Inventor
彭欣欣
夏长久
朱斌
林民
罗一斌
舒兴田
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.)
Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
Original Assignee
Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
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 Sinopec Research Institute of Petroleum Processing, China Petroleum and Chemical Corp filed Critical Sinopec Research Institute of Petroleum Processing
Priority to CN202010747645.7A priority Critical patent/CN114057549B/en
Publication of CN114057549A publication Critical patent/CN114057549A/en
Application granted granted Critical
Publication of CN114057549B publication Critical patent/CN114057549B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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
    • C07C37/60—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by oxidation reactions introducing directly hydroxy groups on a =CH-group belonging to a six-membered aromatic ring with the aid of other oxidants than molecular oxygen or their mixtures with molecular oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/80—Mixtures of different zeolites
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • B01J29/7049—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing rare earth elements, titanium, zirconium, hafnium, zinc, cadmium, mercury, gallium, indium, thallium, tin or lead
    • B01J29/7057—Zeolite Beta
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/89—Silicates, aluminosilicates or borosilicates of titanium, zirconium or hafnium
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Abstract

A method for simultaneously preparing phenol and benzenediol is characterized in that benzene, secondary alcohol, hydrogen peroxide and a composite catalyst are contacted to obtain a product containing phenol and benzenediol. Wherein the composite catalyst comprises an oxidation catalytic active center and an MPV reaction catalytic active center. The method has the advantages of simple reaction process, high raw material conversion rate, high product yield and low byproduct selectivity.

Description

Method for simultaneously preparing phenol and benzenediol
Technical Field
The present invention relates to the field of organic synthesis, and more particularly to a process for the simultaneous preparation of phenol and benzenediol.
Background
Phenol and benzenediol (catechol, hydroquinone) are important chemical intermediates. At present, industrial phenol is mainly prepared by a cumene method, and although the phenol production process by the cumene method is mature, the problems of complex process flow, serious equipment corrosion, more byproducts, overlarge energy consumption in the refining process, unstable intermediate product CHP (cumene peroxide) and the like exist. The production of the benzenediol comprises a Rhone-Poulenc method, a Brishima method and a Ube method, but the method has the problems of difficult recovery of homogeneous reaction catalysts, high raw material unit consumption and low benzenediol selectivity.
The benzene can be directly oxidized by using hydrogen peroxide as an oxidant to obtain phenol and benzenediol, and the benzenediol can be oxidized by using hydrogen peroxide.
CN101302141a discloses a method for directly synthesizing phenol by using liquid-phase benzene oxide with vanadium-loaded SBA-16 as catalyst and molecular oxygen as oxidant, the benzene conversion rate is 15.4-28.2% after 5h reaction, and the selectivity of phenol is 70-80%.
CN102274755a discloses a method for synthesizing Schiff base copper/heteropolyacid supermolecular compound loaded on silicon-based molecular sieve, the compound can be directly applied in the reaction of synthesizing phenol by direct oxidation of benzene, the yield of phenol is 16.4% after 6h of reaction, and the selectivity is 91.2%.
CN 102627530a discloses a method for preparing phenol and benzenediol by catalytic hydroxylation of benzene with pigment green B (naphthol ligand complex of organometallic iron) as catalyst, acetonitrile as solvent, and hydrogen peroxide as oxidant. The benzene conversion rate of the reaction for 5 hours is 26.5 percent, and the yields of phenol, catechol and hydroquinone are 12.2 percent, 3.3 percent and 4.6 percent respectively.
The advent of titanium silicalite molecular sieves has provided a new route to the preparation of phenol and benzenediol by the mild oxidation of benzene. EP 0894783 discloses a method for preparing phenol by catalyzing benzene hydroxylation under the conditions of taking a titanium-silicon molecular sieve as a catalyst, hydrogen peroxide as an oxidant and water as a solvent, but the conversion rate of benzene is only 1-2%.
CN101759530a discloses a method for preparing benzene diphenol by catalytic hydroxylation under the condition of taking titanium-silicon molecular sieve TS-1 as a catalyst, hydrogen peroxide as an oxidant and water as a solvent, wherein the selectivity of benzene diphenol in the product is 96%, and the effective utilization rate of hydrogen peroxide is 55%.
CN101659599a discloses a method for synthesizing phenol by catalyzing benzene and hydrogen peroxide with a modified TS-1 molecular sieve, acetonitrile is selected as a solvent, the reaction is carried out for 4 hours at 70 ℃, the conversion rate of the obtained benzene can reach 10%, and the selectivity of the phenol can reach 90%.
CN107400051a discloses a method for preparing p-benzoquinone by titanium silicalite molecular sieve, which is to react TS-1 molecular sieve, hydrogen peroxide and benzene to generate p-benzoquinone.
Parabenzoquinone, tar and the like are deeply oxidized products, and the selectivity of phenol and benzenediol produced is reduced as byproducts, however, in the existing technology for preparing phenol and benzenediol by catalyzing and oxidizing benzene with a titanium silicon molecular sieve, few reports are about how to reduce the deeply oxidized reaction products such as parabenzoquinone, tar and the like.
Disclosure of Invention
The invention aims to solve the problems of high byproduct selectivity, deep reaction of target products, low yields of phenol and benzenediol and the like in the existing method, and provides a method for preparing phenol and benzenediol simultaneously, which is different from the prior art.
Based on a large number of experiments and analysis of the reaction process of benzene oxidation, the inventor finds that the process of oxidizing benzene into phenol, further oxidizing phenol into benzenediol (catechol and hydroquinone), oxidizing benzenediol into quinone and further oxidizing the benzenediol into tar is a series reaction, and under the condition of oxidation reaction, products are difficult to stay in the phenol and benzenediol stages, so that the selectivity of byproducts is high and the yield of target products is low. It is therefore necessary to interrupt the progress of the deep oxidation reaction to obtain a high yield of the desired product.
The method for simultaneously preparing phenol and benzenediol is characterized in that benzene, secondary alcohol, hydrogen peroxide and a compound catalyst are contacted and reacted to obtain a product containing phenol and benzenediol, wherein the compound catalyst comprises a catalyst containing an oxidation reaction catalytic active center and a catalyst containing an MPV reaction catalytic active center.
In the present invention, the composite catalyst is preferably composed of a catalyst containing an oxidation reaction catalytic active site and a catalyst containing an MPV reaction catalytic active site.
In the composite catalyst, the catalyst containing the catalytic active center of the oxidation reaction is the catalytic active center capable of activating hydrogen peroxide and catalyzing the oxidation of organic molecules, or the catalytic active center capable of catalyzing the oxidation of hydrogen peroxide and organic molecules to obtain the oxygen-containing organic compound. The catalyst containing the catalytic active center of the oxidation reaction can be a titanium-containing catalytic material with a micropore, mesopore or macropore structure, preferably a titanium silicalite molecular sieve, more preferably a titanium silicalite molecular sieve with a MFI, MEL, MWW, MOR, BEA, CON, EWT, MSE, ITN, IFR, DON, CFI, UTL, OKO and hexagonal mesopore structure, and still more preferably a titanium silicalite molecular sieve (TS-1) with an MFI structure. The molar ratio of titanium to silicon element in the titanium-silicon molecular sieve phase is preferably (0.005-0.04): 1. further preferably (0.001-0.03): 1. more preferably (0.015-0.025): 1.
in the composite catalyst of the present invention, the catalyst containing an MPV reaction catalytic active center refers to a catalytic active center capable of catalyzing an MPV reaction. MPV (Meerwein-Ponndorf-Verley) reaction refers to the reaction of a ketone and a secondary alcohol under the catalysis of a Lewis acid to form the corresponding alcohol and ketone. Tin or zirconium is preferred as the catalytic active center for the MPV reaction in the present invention. The catalyst containing the MPV reaction catalytic active center is preferably a molecular sieve type catalytic material, for example, a tin-silicon or zirconium-silicon molecular sieve having a MFI, MEL, MWW, MOR, BEA, CON, EWT, MSE, ITN, IFR, DON, CFI, UTL, OKO or hexagonal mesoporous structure, more preferably a tin-silicon or zirconium-silicon molecular sieve having a BEA structure, and even more preferably a Zr- β molecular sieve having a BEA structure. The Zr-beta molecular sieve with BEA structure at least contains silicon, oxygen, zirconium and hydrogen elements, more preferably, the mole ratio of zirconium to silicon at the surface part of the Zr-containing molecular sieve is higher than that at the central part of the molecular sieve, and the mole ratio of zirconium to silicon in the molecular sieve phase is (0.001-0.04): 1. The ratio of the molar ratio of zirconium to silicon at the surface site of the molecular sieve to the molar ratio of zirconium to silicon at the central site of the molecular sieve is, for example, (1.5-200): 1, preferably (5-100): 1, more preferably (10-70): 1, most preferably (20-50): 1.
in the invention, the Zr-containing molecular sieve mainly enriches zirconium element in the molecular sieveThe surface is the surface zirconium-rich molecular sieve. The molar ratio of zirconium to silicon at the surface part of the molecular sieve and the molar ratio of zirconium to silicon at the central part of the molecular sieve are respectively determined by TEM energy spectrum characterization, and a rectangular selected area at the surface part of the molecular sieve and a rectangular selected area at the central part of the molecular sieve of a TEM morphology picture of the molecular sieve crystal grain are respectively selected as target points for composition analysis; wherein, the rectangular selective area of the surface part of the molecular sieve is to make a tangent line on the boundary of the molecular sieve crystal grain, select an area which is perpendicular to the tangent line and has a distance of less than 10nm, the rectangular selective area is located in the area, and the overlapping area of the rectangular selective area and the molecular sieve crystal grain is 50-3000 nm 2 The method comprises the steps of carrying out a first treatment on the surface of the The rectangular selective area at the central part of the molecular sieve takes the grain boundary of the molecular sieve as the boundary of the maximum inscribed circle and takes 50 percent of the radius of the inscribed circle as the concentric circle, the rectangular selective area is positioned in the concentric circle, and the area of the rectangular selective area is 50-3000 nm 2 . When TEM energy spectrum characterization is measured, rectangular selected areas with the same area are selected at the surface part and the central part.
The surface zirconium-rich molecular sieve is not limited to the type and content of other elements, for example, the molecular sieve can also contain at least one element of aluminum, boron, titanium, tin, vanadium, cobalt, chromium, hafnium, tantalum, tungsten and lead, and the molar ratio of the element to silicon is (0-0.04): 1, preferably zirconium alone is the heteroatom element.
In the invention, the catalyst of the MPV reaction catalytic active center in the composite catalyst is preferably a surface zirconium-rich heteroatom molecular sieve, and the surface zirconium-rich heteroatom molecular sieve is preferably prepared by a method comprising the steps of contacting a molecular sieve N with skeleton hydroxyl vacancies with a polyhydroxy compound, separating to obtain a molecular sieve O, contacting the molecular sieve O with a zirconium source-containing liquid P, and recovering a product.
The molecular sieve N with skeleton hydroxyl vacancy can be obtained by adopting direct synthesis such as hydrothermal synthesis method, or can be obtained by adopting post-treatment such as removing part of skeleton atoms, for example, acid treatment, alkali treatment, high-temperature hydrothermal treatment or microwave treatment and other methods are adopted to remove part of skeleton atoms. Preferably by a post-treatment process. Preferably, the parent molecular sieve used in the post-treatment is a silica-alumina molecular sieve.
The skeleton hydroxyl vacancy refers to the infrared hydroxyl spectrum of the material with the wave number of 3550cm -1 There are distinct characteristic peaks in the vicinity. In the infrared hydroxyl spectrogram of the molecular sieve, 3550cm -1 The nearby signal peak can characterize the nest hydroxyl group, 3735cm -1 The nearby signal peaks may characterize the terminal hydroxyl groups. The molecular sieve N is a silicon-aluminum molecular sieve, and the infrared hydroxyl spectrogram of the molecular sieve N is 3735cm after part of framework atoms are removed -1 Characteristic peak intensity (in terms of peak height) and wavenumber at 3550cm -1 Ratio I of nearby characteristic peak intensities (in terms of peak heights) 3735 /I 3550 4-10.
The polyhydroxy compound preferably has a carbon number of C2-C12, more preferably C5-C8, and a hydroxyl number of at least 2, and further preferably has hydroxyl groups on adjacent carbon atoms. Illustrative but non-exhaustive polyols may be one or more of ethylene glycol, propylene glycol, butylene glycol, pentylene glycol, hexylene glycol, heptylene glycol, octylene glycol, nonylene glycol, decylene glycol, undecylene glycol, dodecylene glycol, glycerol, butanetriol, pentylmethanol, hexanetriol, octatetrol, cyclopentanediol, cyclohexanediol, cycloheptanediol, cyclooctadecylene glycol, cycloundecylene glycol, cyclododecylene glycol, benzenediol (e.g., catechol, hydroquinone, resorcinol), methylbenzenediol, ethylbenzenediol, naphthalenediol, tricarbosaccharides (e.g., dihydroxyacetone), tetracarbonates, pentasaccharides (e.g., ribose, deoxyribose, ribulose), hexasaccharides (e.g., glucose, fructose), heptose, oligosaccharides (e.g., sucrose, maltose, lactose, cellobiose), or isomers thereof.
The polyhydroxy compound is a liquid containing polyhydroxy compound, and the mass fraction of the polyhydroxy compound in the liquid is 20-100%; the polyol-containing liquid may contain a solvent for dissolving the polyol, and the solvent is preferably a C1-C10 alcohol, ketone, ether or ester. Preferably, the polyol-containing liquid is free of solvent.
The contact of the molecular sieve N with skeleton hydroxyl vacancies and the polyhydroxy compound is carried out under the conditions of 5-100 ℃, preferably 40-80 ℃,0.01-5MPa, preferably normal pressure, and the pressure is absolute pressure. The volume ratio of the polyol-containing liquid to the molecular sieve N is preferably (1-100): 1, more preferably (5-70): 1, still more preferably (10-40): 1. The contact time may be 5min to 24h, preferably 1h to 4h. The contacting may be immersing, mixing and stirring, and the fluid passing, the separating may be filtering and centrifuging, and the invention is not particularly limited.
The zirconium source is an organic zirconium source and/or an inorganic zirconium source. Wherein the organic zirconium source is selected from zirconium n-propoxide, zirconium isopropoxide, zirconium n-butoxide, zirconocene dichloride, zirconium acetate, zirconium propionate, zirconium tetrabenzyl, zirconium tetra (ethylmethylamino) dichloride (IV), zirconium tetramethyl acrylate, zirconium hexafluoro-acetylacetonate, zirconium chlorodicyclopentadiene, tetrabutyl zirconate, zirconium acetylacetonate, zirconium bis (n-butylcyclopentadienyl) dichloride, zirconium cyclopentadienyl trichloride, zirconium tetra (dimethylamino) 1, 1-trifluoroacetylacetonate, zirconium pentamethylcyclopentadienyl trichloride (IV), zirconium tetraethoxide, zirconium tetra (2, 6-tetramethyl-3, 5-heptanedioate), zirconium bis (pentamethylcyclopentadienyl) dichloride, rac-ethylene bis (1-indenyl) zirconium dichloride, zirconium isooctanoate, bis (cyclopentadienyl) dimethylzirconium, bis (cyclopentadienyl) zirconium hydride, zirconium tert-butoxide, bis (methylcyclopentadienyl) dichloride, bis [ carbonate ] diammonium zirconium dichloride, bis (methyl) cyclopentadienyl) dicyclopentadiene dichloride, bis (T-cyclopentadienyl) dicyclopentadiene, bis (cyclopentadienyl) bis (3-zirconium) di (methyl) cyclopentadienyl) dichloride, bis (cyclopentadienyl) bis (3-zirconium) di (isopropyl) dichloride, bis (cyclopentadienyl) zirconium (1-bis (isopropyl) dichloride; the inorganic zirconium source is one or more selected from zirconium tetrachloride, zirconium sulfate, zirconium nitrate, zirconyl nitrate, zirconium carbonate, zirconium fluoride, ammonium fluorozirconate, potassium fluorozirconate, zirconium hydroxide and zirconium oxychloride.
The zirconium source-containing liquid P contains a zirconium source-soluble solvent selected from alcohols, ketones, ethers, esters, water, etc. having C1-C10. Preferably C1-C6 alcohols, ketones, ethers, esters, the source of in the zirconium-containing liquid may be present in an amount of 5-30%, preferably 10-20% by mass.
The contact of the molecular sieve O with the liquid P containing the zirconium source is carried out at 5-100 ℃, preferably 30-60 ℃,0.01-5MPa, preferably at normal pressure, the pressure is absolute pressure, and the contact time is preferably 5-360min. The contacting may be performed by solid-liquid contact such as dipping, mixing and stirring. The zirconium element in the liquid P and the molecular sieve O (SiO 2 The molar ratio may be (0.001-0.04): 1, preferably (0.005-0.02): 1, more preferably (0.008-0.015): 1.
The recovery of the product includes centrifugation, filtration, evaporation, such as preferably evaporation of the solvent at atmospheric or reduced pressure. The recovered product may further comprise a drying step at a temperature of 60 to 200 c, preferably 80 to 150 c, more preferably 100 to 130 c, under vacuum or atmospheric conditions, and a calcination step at an oxygen-depleted or oxygen-enriched, 300 to 800 c, preferably 400 to 700 c, more preferably 500 to 600 c.
In the invention, the composite catalyst is obtained by mechanically mixing or molding a catalyst containing an oxidation reaction catalytic active center and a catalyst containing an MPV reaction catalytic active center.
In the method of the invention, the composite catalyst can be one or more molecular sieves which simultaneously contain an oxidation reaction catalytic active center and an MPV reaction catalytic active center, or two molecular sieves which respectively contain an oxidation reaction catalytic active center and an MPV reaction catalytic active center, preferably two molecular sieves which respectively contain an oxidation reaction catalytic active center and an MPV reaction catalytic active center. The catalyst containing the catalytic active center of the oxidation reaction and the catalyst containing the catalytic active center of the MPV reaction can be used in a mechanical mixing mode or can be prepared into a catalyst in a molding mode for use. Since the catalyst forming process involves the prior art, the present invention is not repeated.
In the method of the invention, the ratio of the catalytic active center of the oxidation reaction to the catalytic active center of the MPV reaction has an optimal interval, and the two active centers are matched with each other to be more beneficial to promoting the conversion of benzene to generate phenol and benzenediol, wherein the ratio of the molar number of the catalytic active center of the oxidation reaction to the catalytic active center of the MPV reaction is preferably 1: (0.2-1), preferably 1: (0.3-0.8), more preferably 1: (0.4-0.6).
In the process of the present invention, the secondary alcohol is preferably a secondary alcohol having 3 to 10 carbon atoms, including isopropanol, sec-butanol, 2-pentanol, 3-methyl-2-butanol, 2-hexanol, 3-methyl-2-pentanol, 3-hexanol, 2-methyl-3-pentanol, 2-heptanol, 3-heptanol, 4-heptanol, 2-octanol, 3-octanol, 4-octanol, cyclopentanol, methylcyclopentanol, cyclohexanol, preferably isopropanol, sec-butanol, 2-pentanol, 3-pentanol.
In the process of the invention, the molar ratio of benzene to secondary alcohol is preferably 1: (5-100), further preferably 1: (10-80), more preferably 1: (20-50); the molar ratio of benzene to hydrogen peroxide is preferably 1: (0.1 to 5), further preferably 1: (0.8-4), more preferably 1: (1.5-3); the weight ratio of the oxidation reaction catalyst to benzene in the composite catalyst is preferably (0.01-0.3): 1, further preferably (0.05-0.2): 1, more preferably (0.07-0.15): 1, a step of; the reaction temperature is preferably 40 to 100 ℃, further preferably 60 to 80 ℃; the reaction time is preferably 5min to 24h.
The process of the present invention may be carried out under normal pressure or under elevated pressure, for example, under a gauge pressure of 0 to 5MPa, and the present invention is not particularly limited, and is preferably carried out under normal pressure. The method of the present invention may be carried out in a tank reactor, a fixed bed reactor, a moving bed reactor, a microchannel reactor, and the present invention is not particularly limited. The composite catalyst used in the invention can recover part or all of the catalyst after the reaction by centrifugation, filtration and other methods, and is used for the next reaction after drying, roasting or direct recovery, and no special requirement is required for the recycling process of the catalyst.
The method for simultaneously preparing phenol and benzenediol has the characteristics of simple reaction process, mild reaction conditions and easy implementation, and the yields of phenol and benzenediol are high.
Drawings
FIG. 1 shows the results of FT-IR tests on beta molecular sieves N with backbone hydroxyl vacancies in the pre-preparation, 3550cm -1 The nearby signal peak can characterize the nest hydroxyl group, 3735cm -1 The nearby signal peaks may characterize the terminal hydroxyl groups.
FIG. 2 is a representation of the spectral microzone of a transmission electron microscope of a sample of a molecular sieve of preparation example.
Detailed Description
The invention is further illustrated by the following examples, which are not intended to limit the scope of the invention.
In the following examples and comparative examples, infrared hydroxy spectra were obtained using KBr pellets and measured using FT-IR spectroscopy, scanning in the range 400-4000cm-1; the chemical composition was tested using XRF method; the zirconium element distribution adopts a transmission electron microscope-energy spectrum method to carry out micro-region composition analysis on the molecular sieve crystal grains.
All raw materials are analytically pure reagents unless otherwise specified.
The reaction product is analyzed by gas chromatography, and the analysis result is quantified by an internal standard method. The chromatographic conditions were: agilent-6890 chromatograph, 30m×0.25mm HP-5 capillary column, sample injection amount 0.5 μL, sample injection port temperature 280 ℃. The column temperature was maintained at 100deg.C for 2min, then raised to 280℃at a rate of 15deg.C/min, and maintained for 3min. FID detector, detector temperature 300 ℃.
The reaction possibly occurs in the reaction process of benzene and hydrogen peroxide:
benzene + hydrogen peroxide → phenol + water
Phenol + hydrogen peroxide- & gt catechol/hydroquinone + water
Benzene + hydrogen peroxide → p-benzoquinone + water
Hydroquinone + hydrogen peroxide → p-benzoquinone + water
In each of the examples and comparative examples:
total phenol (phenol+benzenediol) yield Y (%) = (n (phenol) +n (catechol) +n (hydroquinone))/n 0 (benzene) ×100%
Wherein Y is the yield, n is the molar amount of the substance in the product, and n0 is the molar amount of the starting substance of the reaction.
Preparation example
This pre-preparation example is used to illustrate the preparation of beta molecular sieves N having a backbone hydroxyl vacancy.
50g (dry basis) of silicon-aluminum beta molecular sieve (silicon-aluminum ratio is 11) is added with water to prepare a molecular sieve solution with the solid content of 10 weight percent, and 13mol/LHNO is added in stirring 3 Heating to 100 ℃, stirring for 20 hours at constant temperature, filtering, washing with water until the filtrate is neutral, drying, and roasting at 550 ℃ for 2 hours to obtain the beta molecular sieve N with skeleton hydroxyl vacancies.
And (3) carrying out XRF and FT-IR analysis tests on the beta molecular sieve and the beta molecular sieve N before and after the nitric acid dealumination treatment. The FT-IR spectrum of the beta molecular sieve N is shown in FIG. 1, and can be seen at 3550cm -1 The vicinity has characteristic peaks which indicate that part of framework aluminum of the molecular sieve is removed, I 3735 /I 3550 4.3, and the silicon-aluminum ratio of the beta molecular sieve N after dealumination treatment is 1650.
Preparation examples 1-12 illustrate the preparation of catalysts containing MPV reaction catalytic active sites.
Preparation example 1
The beta molecular sieve N obtained in the preparation example is mixed with 1, 2-hexanediol according to the volume ratio of 1:10, treated for 2 hours at 60 ℃ and normal pressure, and then filtered to obtain the molecular sieve O1.
Zirconium oxychloride is mixed with ethanol to obtain a liquid P1 containing a zirconium source, wherein the mass fraction of the zirconium oxychloride is 20%, and then the liquid P1 and the molecular sieve O1 are mixed and treated for 30 minutes at 50 ℃ under normal pressure, wherein the molar ratio of zirconium element to the molecular sieve O1 (calculated by SiO 2) in the liquid P1 is 0.01:1. And (3) evaporating the solvent under reduced pressure to obtain molecular sieve solid, drying at 120 ℃ for 12 hours, and roasting at 550 ℃ for 6 hours to obtain a Zr-beta molecular sieve sample with the surface rich in zirconium, wherein the number is R1.
XRF and transmission electron microscopy spectra characterization was performed on R1, and the results are shown in fig. 2 and table 1.
Preparation example 2
The molecular sieve N obtained in the preparation example is mixed with 1, 2-cyclohexanediol according to the volume ratio of 1:30, treated for 1h at 40 ℃ under normal pressure, and then filtered to obtain the molecular sieve O2.
Zirconium tetrachloride and ethanol are mixed to obtain a liquid P2 containing a zirconium source, wherein the mass fraction of the zirconium tetrachloride is 10%, and then the liquid P2 and the molecular sieve O2 are mixed and treated for 60 minutes at the temperature of 30 ℃ and under the normal pressure, wherein the mol ratio of zirconium element to the molecular sieve O2 (calculated by SiO 2) in the liquid P2 is 0.008:1. And (3) evaporating the solvent under reduced pressure to obtain molecular sieve solid, drying at 110 ℃ for 12 hours, and roasting at 500 ℃ for 12 hours to obtain a Zr-beta molecular sieve sample with the surface rich in zirconium, wherein the number is R2.
XRF and transmission electron spectroscopy characterization was performed on R2, and the results are shown in table 1.
Preparation example 3
The molecular sieve N obtained in the preparation example is mixed with 1, 2-octanediol according to the volume ratio of 1:20, treated for 3 hours at 80 ℃ and normal pressure, and then centrifuged to obtain the molecular sieve O3.
Zirconium n-propoxide and n-propanol are mixed to obtain a liquid P3 containing a zirconium source, wherein the mass fraction of the zirconium n-propoxide is 15%, and then the liquid P3 and the molecular sieve O3 are mixed and treated for 120min under the conditions of 60 ℃ and normal pressure, wherein the molar ratio of zirconium element to the molecular sieve O3 (calculated as SiO 2) in the liquid P3 is 0.013:1. Evaporating the solvent to obtain molecular sieve solid, further drying at 150 ℃ for 6 hours, and roasting at 500 ℃ for 6 hours to obtain Zr-beta molecular sieve sample with zirconium-enriched surface, number R3.
XRF and transmission electron microscopy spectra characterization was performed on R3 and the results are shown in table 1.
Preparation example 4
The molecular sieve N obtained in the preparation example is mixed with 1, 2-hexanediol according to the volume ratio of 1:40, treated for 4 hours at 50 ℃ and normal pressure, and then centrifuged to obtain the molecular sieve O4.
Zirconium oxychloride is mixed with methanol to obtain a liquid P4 containing a zirconium source, wherein the mass fraction of the zirconium oxychloride is 20%, and then the liquid P4 and the molecular sieve O4 are mixed and treated for 90 minutes at 40 ℃ under normal pressure, wherein the molar ratio of zirconium element to the molecular sieve O4 (calculated as SiO 2) in the liquid P4 is 0.01:1. And (3) evaporating the solvent under reduced pressure to obtain molecular sieve solid, further drying at 120 ℃ for 6 hours, and roasting at 550 ℃ for 6 hours to obtain a Zr-beta molecular sieve sample with the surface rich in zirconium, wherein the number is R4.
XRF and transmission electron spectroscopy characterization was performed on R4 and the results are shown in table 1.
Preparation example 5
The molecular sieve N obtained in the preparation example is mixed with 1, 2-cyclopentanediol according to the volume ratio of 1:10, treated for 3 hours at 60 ℃ and normal pressure, and then centrifuged to obtain the molecular sieve O5.
Zirconium nitrate and butanone are mixed to obtain liquid P5 containing a zirconium source, wherein the mass fraction of the zirconium nitrate is 15%, and then the liquid P5 and the molecular sieve O5 are mixed and treated for 180 minutes under the conditions of 30 ℃ and normal pressure, wherein the mol ratio of zirconium element to the molecular sieve O5 (calculated as SiO 2) in the liquid P5 is 0.015:1. And (3) evaporating the solvent under reduced pressure to obtain molecular sieve solid, further drying at 100 ℃ for 3 hours, and roasting at 550 ℃ for 6 hours to obtain a Zr-beta molecular sieve sample with the surface rich in zirconium, wherein the number is R5.
XRF and transmission electron microscopy spectra characterization was performed on R5 and the results are shown in table 1.
Preparation example 6
The molecular sieve N obtained in the preparation example is mixed with 1, 2-butanediol according to the volume ratio of 1:50, the mixture is treated for 5 hours at the temperature of 30 ℃ and under the normal pressure, and then the molecular sieve O6 is obtained by filtration.
Mixing zirconium oxychloride with ethanol to obtain a liquid P6 containing a zirconium source, wherein the mass fraction of the zirconium oxychloride is 30%, and mixing the liquid P6 with a molecular sieve O6 at 80 ℃ and under normal pressure for 30min, wherein the molar ratio of zirconium element in the liquid P6 to the molecular sieve O6 (calculated as SiO 2) is 0.01:1. And (3) evaporating the solvent under reduced pressure to obtain molecular sieve solid, further drying at 120 ℃ for 12 hours, and roasting at 550 ℃ for 6 hours to obtain a Zr-beta molecular sieve sample with the surface rich in zirconium, wherein the number is R6.
XRF and transmission electron microscopy spectra characterization was performed on R6 and the results are shown in table 1.
Preparation example 7
The molecular sieve N obtained in the preparation example is mixed with 1, 2-propylene glycol according to the volume ratio of 1:60, the mixture is treated for 8 hours at the temperature of 10 ℃ and under the normal pressure, and then the molecular sieve O7 is obtained by filtration.
Zirconium nitrate and ethyl acetate are mixed to obtain a liquid P7 containing a zirconium source, wherein the mass fraction of the zirconium nitrate is 5%, and then the liquid P7 and the molecular sieve O7 are mixed and treated for 60 minutes under the conditions of 20 ℃ and normal pressure, wherein the mol ratio of zirconium element to the molecular sieve O7 (calculated as SiO 2) in the liquid P7 is 0.005:1. And (3) evaporating the solvent under reduced pressure to obtain molecular sieve solid, further drying at 140 ℃ for 12 hours, and roasting at 550 ℃ for 6 hours to obtain a Zr-beta molecular sieve sample with the surface rich in zirconium, wherein the number is R7.
XRF and transmission electron spectroscopy characterization was performed on R7 and the results are shown in table 1.
Preparation example 8
The molecular sieve N obtained in the preparation example is mixed with 1, 4-butanediol according to the volume ratio of 1:80, the mixture is treated for 6 hours at 20 ℃ under normal pressure, and then the molecular sieve O8 is obtained by filtration.
Zirconium n-propoxide and acetone are mixed to obtain a liquid P8 containing a zirconium source, wherein the mass fraction of the zirconium n-propoxide is 25%, and then the liquid P8 and the molecular sieve O8 are mixed and treated for 120min under the conditions of 70 ℃ and normal pressure, wherein the molar ratio of zirconium element to the molecular sieve O8 (calculated as SiO 2) in the liquid P8 is 0.02:1. And (3) evaporating the solvent under reduced pressure to obtain molecular sieve solid, drying at 100 ℃ for 18h, and roasting at 600 ℃ for 6h to obtain a Zr-beta molecular sieve sample with the surface rich in zirconium, wherein the number is R8.
XRF and transmission electron spectroscopy characterization was performed on R8 and the results are shown in table 1.
Preparation example 9
The molecular sieve N obtained in the preparation example is mixed with glycerin according to the volume ratio of 1:70, and is treated for 24 hours at the temperature of 100 ℃ and under normal pressure, and then the molecular sieve O9 is obtained by filtration.
Zirconium oxychloride is mixed with methanol to obtain liquid P9 containing a zirconium source, wherein the mass fraction of the zirconium oxychloride is 8%, and then the liquid P9 and the molecular sieve O9 are mixed and treated for 120min at 80 ℃ under normal pressure, wherein the mol ratio of zirconium element to the molecular sieve O9 (calculated as SiO 2) in the liquid P9 is 0.015:1. And (3) evaporating the solvent under reduced pressure to obtain molecular sieve solid, drying at 110 ℃ for 5 hours, and roasting at 550 ℃ for 6 hours to obtain a Zr-beta molecular sieve sample with the surface rich in zirconium, wherein the number is R9.
XRF and transmission electron microscopy spectra characterization was performed on R9 and the results are shown in table 1.
Preparation example 10
Mixing the molecular sieve N obtained in the preparation example with a mixture of naphthalene diphenol and ethanol according to a volume ratio of 1:50, wherein the mass fraction of naphthalene diphenol in the mixture of naphthalene diphenol and ethanol is 50%, standing for 12 hours at 30 ℃ under normal pressure, and filtering to obtain the molecular sieve O10.
Zirconium tetrachloride and butanol are mixed to obtain a liquid P10 containing a zirconium source, wherein the mass fraction of the zirconium tetrachloride is 25%, and then the liquid P10 and the molecular sieve O10 are mixed and treated for 240min under the conditions of 100 ℃ and normal pressure, wherein the molar ratio of zirconium element to the molecular sieve O10 (calculated as SiO 2) in the liquid P10 is 0.04:1. Evaporating the solvent under reduced pressure to obtain molecular sieve solid, further drying at 120 ℃ for 5 hours, and roasting at 550 ℃ for 12 hours to obtain Zr-beta molecular sieve sample with zirconium-enriched surface, number R10.
XRF and transmission electron spectroscopy characterization was performed on R10 and the results are shown in table 1.
PREPARATION EXAMPLE 11
This preparation example is used to illustrate a hydrothermally synthesized Zr-beta molecular sieve.
Reference methods Zr-beta molecular sieves (RSC adv.,2014,4,13481-13489) were hydrothermally synthesized in a fluorine-containing system. 10.42g of tetraethyl silicate are weighed out, mixed with 10.31g of tetraethyl ammonium hydroxide (40 wt% aqueous solution) and hydrolyzed with stirring. After 2h, 1.55g of an aqueous solution of zirconium oxychloride was added, in a molar ratio of zirconium to silicon of 0.01:1. After stirring the resulting mixture for a further 8 hours, a further 1.215ml of HF solution (40% by weight) and 0.105g of pure silicon beta molecular sieve were added as seed crystals. Crystallizing the obtained mixture at 140 ℃ for 20 days, filtering and washing to obtain a solid product, drying the solid product at 120 ℃ for 12 hours, and roasting at 550 ℃ for 6 hours to obtain a conventional Zr-beta molecular sieve sample, and the number is D1.
XRF and transmission electron microscopy spectra characterization was performed on D1 molecular sieves, and the results are shown in table 1.
Preparation example 12
This preparation example is used to illustrate Zr-beta molecular sieves prepared by post-synthesis zirconium intercalation.
Zirconium oxychloride is mixed with ethanol to obtain liquid P11 containing a zirconium source, wherein the mass fraction of the zirconium oxychloride is 20%, and then the liquid P11 and the molecular sieve N of the preparation example are mixed for 30min at 50 ℃ under normal pressure, wherein the mol ratio of zirconium element to the molecular sieve O1 (calculated as SiO 2) in the liquid P11 is 0.01:1. And then decompressing and evaporating the solvent to obtain molecular sieve solid, further drying the obtained molecular sieve solid at 120 ℃ for 12 hours, and roasting at 550 ℃ for 6 hours to obtain a conventional Zr-beta molecular sieve sample, with the number of D2.
XRF and transmission electron microscopy spectra characterization was performed on D2 molecular sieves and the results are shown in table 1.
TABLE 1
As can be seen from Table 1, the catalyst Zr-beta molecular sieve containing MPV reaction catalytic active center provided by the invention has a surface zirconium-silicon molar ratio higher than that of the central part zirconium-silicon molar ratio, and a surface zirconium-silicon molar ratio of between 10 and 86, and has obvious surface zirconium-rich property; the molecular sieves D1 and D2 obtained in preparation examples 11 and 12 in the prior art have no characteristic of rich zirconium on the surface, and the ratio of the molar ratio of zirconium on the surface to silicon to the molar ratio of zirconium on the central part to silicon is respectively 0.8 and 1.2.
Preparation example 13
Preparation 13 illustrates the preparation of a catalyst TS-1 molecular sieve containing oxidative catalytic active sites.
About 3/4 of a solution of tetrapropylammonium hydroxide (TPAOH, 20 wt%) was added to a solution of Tetraethylorthosilicate (TEOS) to obtain a liquid mixture having a pH of about 13, and then the desired amount of n-butyl titanate [ Ti (OBu) ] was added dropwise to the obtained liquid mixture with vigorous stirring 4 ]Is stirred for 15 minutes. Finally, the remaining TPAOH was slowly added to the mixture and stirred at 348-353K for about 3 hours to give a chemical composition of 0.03TiO 2 ∶SiO 2 ∶0.36TPA∶35H 2 O sol, then crystallization at 443K temperature for 3 days, then filtering the obtained solid, washing with distilled water, and drying at 373K temperature for 5 hours to obtain a TS-1 molecular sieve sample.
Examples 1-19 illustrate the simultaneous preparation of phenol and benzenediol according to the present invention.
Example 1
Benzene, secondary alcohol, hydrogen peroxide (30wt%) and a catalyst are mixed and put into a reaction kettle, wherein the secondary alcohol is isopropanol, the molar ratio of benzene to isopropanol is 1:20, the molar ratio of benzene to hydrogen peroxide is 1:1.5, the weight ratio of an oxidation catalyst to benzene is 0.1:1, the molar ratio of the oxidation catalyst to the active center of an MPV reaction catalyst is 1:0.5, the oxidation catalyst is TS-1 molecular sieve obtained in preparation example 13, and the MPV reaction catalyst is Zr-beta molecular sieve R1 with rich zirconium on the surface obtained in preparation example 1. After the materials are reacted for 6 hours at 80 ℃ under normal pressure, liquid products are separated for quantitative analysis, and the reaction results are shown in Table 2.
Example 2
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst are mixed and put into a reaction kettle, wherein the secondary alcohol is secondary butanol, the molar ratio of benzene to secondary butanol is 1:50, the molar ratio of benzene to hydrogen peroxide is 1:3, the weight ratio of an oxidation catalyst to benzene is 0.15:1, the molar ratio of the oxidation catalyst to the active center of an MPV reaction catalyst is 1:0.4, the oxidation catalyst is the TS-1 molecular sieve obtained in preparation example 13, and the MPV reaction catalyst is the Zr-beta molecular sieve R1 with rich zirconium on the surface obtained in preparation example 1. After the materials were reacted at 70℃for 9 hours under normal pressure, the liquid products were separated and quantitatively analyzed, and the reaction results are shown in Table 2.
Example 3
Benzene, secondary alcohol, hydrogen peroxide (30wt%) and a catalyst are mixed and put into a reaction kettle, wherein the secondary alcohol is 2-amyl alcohol, the molar ratio of benzene to 2-amyl alcohol is 1:30, the molar ratio of benzene to hydrogen peroxide is 1:2, the weight ratio of an oxidation catalyst to benzene is 0.07:1, the molar ratio of the oxidation catalyst to the active center of an MPV reaction catalyst is 1:0.6, the oxidation catalyst is TS-1 molecular sieve obtained in preparation example 13, and the MPV reaction catalyst is Zr-beta molecular sieve R1 with rich zirconium on the surface obtained in preparation example 1. After the materials react for 12 hours at 70 ℃ under normal pressure, liquid products are separated for quantitative analysis, and the reaction results are shown in Table 2.
Example 4
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst are mixed and put into a reaction kettle, wherein the secondary alcohol is isopropanol, the molar ratio of benzene to isopropanol is 1:40, the molar ratio of benzene to hydrogen peroxide is 1:1.5, the weight ratio of an oxidation catalyst to benzene is 0.15:1, the molar ratio of the oxidation catalyst to the active center of an MPV reaction catalyst is 1:0.5, the oxidation catalyst is TS-1 molecular sieve obtained in preparation example 13, and the MPV reaction catalyst is Zr-beta molecular sieve R1 with rich zirconium on the surface obtained in preparation example 1. After the materials are reacted for 6 hours at 80 ℃ under normal pressure, liquid products are separated for quantitative analysis, and the reaction results are shown in Table 2.
Example 5
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst are mixed and put into a reaction kettle, wherein the secondary alcohol is secondary butanol, the molar ratio of benzene to secondary butanol is 1:30, the molar ratio of benzene to hydrogen peroxide is 1:2, the weight ratio of an oxidation catalyst to benzene is 0.1:1, the molar ratio of the oxidation catalyst to the active center of an MPV reaction catalyst is 1:0.4, the oxidation catalyst is the TS-1 molecular sieve obtained in preparation example 13, and the MPV reaction catalyst is the Zr-beta molecular sieve R1 with rich zirconium on the surface obtained in preparation example 1. The materials were reacted at 60℃under normal pressure for 3 hours, and then the liquid products were separated for quantitative analysis, and the reaction results are shown in Table 2.
Example 6
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst are mixed and put into a reaction kettle, wherein the secondary alcohol is isopropanol, the molar ratio of benzene to isopropanol is 1:80, the molar ratio of benzene to hydrogen peroxide is 1:4, the weight ratio of an oxidation catalyst to benzene is 0.05:1, the molar ratio of the oxidation catalyst to the active center of an MPV reaction catalyst is 1:0.8, the oxidation catalyst is TS-1 molecular sieve obtained in preparation example 13, and the MPV reaction catalyst is Zr-beta molecular sieve R1 with rich zirconium on the surface obtained in preparation example 1. After the materials react for 6 hours at 100 ℃ under normal pressure, liquid products are separated for quantitative analysis, and the reaction results are shown in Table 2.
Example 7
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst are mixed and put into a reaction kettle, wherein the secondary alcohol is 2-hexanol, the molar ratio of benzene to 2-hexanol is 1:10, the molar ratio of benzene to hydrogen peroxide is 1:0.8, the weight ratio of an oxidation catalyst to benzene is 0.2:1, the molar ratio of the oxidation catalyst to the active center of an MPV reaction catalyst is 1:0.3, the oxidation catalyst is TS-1 molecular sieve obtained in preparation example 13, and the MPV reaction catalyst is Zr-beta molecular sieve R1 with rich zirconium on the surface obtained in preparation example 1. After the materials were reacted at 50℃for 16 hours under normal pressure, the liquid products were separated and quantitatively analyzed, and the reaction results are shown in Table 2.
Example 8
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst are mixed and put into a reaction kettle, wherein the secondary alcohol is secondary butanol, the molar ratio of benzene to secondary butanol is 1:5, the molar ratio of benzene to hydrogen peroxide is 1:5, the weight ratio of an oxidation catalyst to benzene is 0.01:1, the molar ratio of the oxidation catalyst to the active center of an MPV reaction catalyst is 1:1, the oxidation catalyst is the TS-1 molecular sieve obtained in preparation example 13, and the MPV reaction catalyst is the Zr-beta molecular sieve R1 with the zirconium-enriched surface obtained in preparation example 1. After the materials were reacted at 40℃for 24 hours under normal pressure, the liquid products were separated and quantitatively analyzed, and the reaction results are shown in Table 2.
Example 9
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst were mixed and put into a reaction kettle, and the difference from example 1 is that the MPV reaction catalyst was Zr- β molecular sieve R2 with rich zirconium surface obtained in preparation example 2. The reaction results are shown in Table 2.
Example 10
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst were mixed and put into a reaction kettle, and the difference from example 1 is that the MPV reaction catalyst was Zr-beta molecular sieve R3 with zirconium-rich surface obtained in preparation example 3. The reaction results are shown in Table 2.
Example 11
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst were mixed and put into a reaction kettle, and the difference from example 1 is that the MPV reaction catalyst was Zr- β molecular sieve R4 with zirconium-rich surface obtained in preparation example 4. The reaction results are shown in Table 2.
Example 12
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst were mixed and put into a reaction kettle, and the difference from example 1 is that the MPV reaction catalyst was Zr- β molecular sieve R5 with zirconium-rich surface obtained in preparation example 5. The reaction results are shown in Table 2.
Example 13
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst were mixed and put into a reaction kettle, and the difference from example 1 is that the MPV reaction catalyst was Zr- β molecular sieve R6 with zirconium-rich surface obtained in preparation example 6. The reaction results are shown in Table 2.
Example 14
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst were mixed and put into a reaction kettle, and the difference from example 1 is that the MPV reaction catalyst was Zr- β molecular sieve R7 with zirconium-rich surface obtained in preparation example 7. The reaction results are shown in Table 2.
Example 15
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst were mixed and put into a reaction kettle, and the difference from example 1 is that the MPV reaction catalyst was Zr-beta molecular sieve R8 with rich zirconium surface obtained in preparation example 8. The reaction results are shown in Table 2.
Example 16
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst were mixed and put into a reaction kettle, and the difference from example 1 is that the MPV reaction catalyst was Zr- β molecular sieve R9 with zirconium-rich surface obtained in preparation example 9. The reaction results are shown in Table 2.
Example 17
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst were mixed and put into a reaction vessel, and the difference from example 1 was that the MPV reaction catalyst was Zr- β molecular sieve R10 rich in zirconium on the surface obtained in preparation example 10. The reaction results are shown in Table 2.
Example 18
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst were mixed and put into a reaction vessel, and the difference from example 1 was that the MPV reaction catalyst was the conventional Zr- β molecular sieve D1 obtained in preparation example 11. The reaction results are shown in Table 2.
Example 19
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst were mixed and put into a reaction vessel, and the difference from example 1 was that the MPV reaction catalyst was the conventional Zr- β molecular sieve D2 obtained in preparation example 12. The reaction results are shown in Table 2.
Example 20
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst were mixed and put into a reaction vessel, differing from example 8 in that the MPV reaction catalyst was the conventional Zr- β molecular sieve D1 obtained in preparation example 11. The reaction results are shown in Table 2.
Example 21
Benzene, secondary alcohol, hydrogen peroxide (30 wt%) and a catalyst were mixed and put into a reaction vessel, and the difference from example 8 was that the MPV reaction catalyst was the conventional Zr- β molecular sieve D2 obtained in preparation example 12. The reaction results are shown in Table 2.
Comparative example 1
This comparative example illustrates the reaction results of a catalyst having only catalytic active sites for oxidation reaction in the composite catalyst.
Benzene, secondary alcohol, hydrogen peroxide (30wt%) and a catalyst are mixed and put into a reaction kettle, wherein the secondary alcohol is isopropanol, the molar ratio of benzene to isopropanol is 1:20, the molar ratio of benzene to hydrogen peroxide is 1:1.5, and the weight ratio of an oxidation reaction catalyst to benzene is 0.1:1, wherein the oxidation reaction catalyst is the TS-1 molecular sieve obtained in preparation example 13. After the materials are reacted for 6 hours at 80 ℃ under normal pressure, liquid products are separated for quantitative analysis, and the reaction results are shown in Table 2.
Comparative example 2
This comparative example illustrates the reaction results of a catalyst having only MPV reaction catalytic active sites in the composite catalyst.
Benzene, secondary alcohol, hydrogen peroxide (30wt%) and a catalyst are mixed and put into a reaction kettle, wherein the secondary alcohol is isopropanol, the molar ratio of benzene to isopropanol is 1:20, the molar ratio of benzene to hydrogen peroxide is 1:1.5, and the weight ratio of MPV reaction catalyst to benzene is 0.1:1, wherein the MPV reaction catalyst is the surface zirconium-rich Zr-beta molecular sieve obtained in preparation example 1. After the materials were reacted at 80℃for 6 hours under normal pressure, the liquid products were separated for quantitative analysis, and the results are shown in Table 2.
TABLE 2
/>
As can be seen from Table 2, the method of the present invention uses secondary alcohol as solvent, and the oxidation reaction catalyst active center and MPV reaction active center act on benzene and hydrogen peroxide simultaneously, so that the yield of the target product is higher, and in particular, the yield of hydroquinone can be significantly improved, compared with the catalyst using only the oxidation reaction active center or the catalyst using only the MPV reaction active center.
The preferred embodiments of the present disclosure have been described in detail above with reference to the accompanying drawings, but the present disclosure is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solutions of the present disclosure within the scope of the technical concept of the present disclosure, and all the simple modifications belong to the protection scope of the present disclosure.
In addition, the specific features described in the foregoing embodiments may be combined in any suitable manner, and in order to avoid unnecessary repetition, the present disclosure does not further describe various possible combinations.
Moreover, any combination between the various embodiments of the present disclosure is possible as long as it does not depart from the spirit of the present disclosure, which should also be construed as the disclosure of the present disclosure.

Claims (17)

1. A method for simultaneously preparing phenol and benzenediol is characterized in that benzene, secondary alcohol, hydrogen peroxide and a composite catalyst are contacted and reacted to obtain a product containing phenol and benzenediol, wherein the composite catalyst comprises a catalyst containing an oxidation reaction catalytic active center and a catalyst containing an MPV reaction catalytic active center;
the catalyst containing the catalytic active center of the oxidation reaction is a titanium-silicon molecular sieve with an MFI structure;
the catalyst containing the MPV reaction catalytic active center is a Zr-beta molecular sieve with a BEA structure, the Zr-beta molecular sieve with the BEA structure at least contains silicon, oxygen, zirconium and hydrogen elements, the molar ratio of zirconium to silicon at the surface part of the molecular sieve is higher than that of zirconium to silicon at the central part, and the molar ratio of zirconium to silicon in the molecular sieve phase is (0.001-0.04): 1; the molar ratio of zirconium to silicon at the surface part of the molecular sieve and the molar ratio of zirconium to silicon at the central part of the molecular sieve are determined by TEM energy spectrum characterization, and a rectangular selected area at the surface part of the molecular sieve and a rectangular selected area at the central part of the molecular sieve are respectively selected as TEM morphology pictures of the molecular sieve crystal grainsPerforming composition analysis for the target spot; the rectangular selective area of the molecular sieve surface part is that a tangent line is made on the boundary of the molecular sieve crystal grain, a region which is perpendicular to the tangent line and has a distance of less than 10nm is selected, the rectangular selective area falls in the region, and the overlapping area of the rectangular selective area and the molecular sieve crystal grain is 50-3000 nm 2 The method comprises the steps of carrying out a first treatment on the surface of the The rectangular selective area at the center of the molecular sieve takes the grain boundary of the molecular sieve as the boundary of the maximum inscribed circle and takes 50 percent of the radius of the inscribed circle as the concentric circle, the shape selective area is positioned in the concentric circle, and the area of the rectangular selective area is 50-3000 nm 2 The molar ratio of zirconium to silicon at the surface part of the molecular sieve to the molar ratio of zirconium to silicon at the central part of the molecular sieve is (10-70): 1.
2. the process according to claim 1, wherein the molar ratio of titanium to elemental silicon in the titanium silicalite phase of the MFI structure is (0.005-0.04): 1.
3. the process according to claim 2, wherein the molar ratio of titanium to elemental silicon in the titanium silicalite phase of the MFI structure is (0.015-0.025): 1.
4. the process according to claim 1, wherein the ratio of the molar ratio of zirconium to silicon at the surface sites of the molecular sieve to the molar ratio of zirconium to silicon at the central sites of the molecular sieve is (20-50): 1.
5. the method according to claim 1, wherein the composite catalyst is obtained by mechanically mixing or shaping a catalyst containing an oxidation reaction catalytic active site and a catalyst containing an MPV reaction catalytic active site.
6. The method according to claim 1, wherein the ratio of the number of moles of the oxidative catalytic active sites to the number of moles of the MPV catalytic active sites is 1: (0.2-1).
7. The process according to claim 1, wherein the secondary alcohol is a secondary alcohol having 3 to 10 carbon atoms.
8. The process according to claim 1, wherein the secondary alcohol is selected from one or more of isopropanol, sec-butanol, 2-pentanol, 3-methyl-2-butanol, 2-hexanol, 3-methyl-2-pentanol, 3-hexanol, 2-methyl-3-pentanol, 2-heptanol, 3-heptanol, 4-heptanol, 2-octanol, 3-octanol, 4-octanol, cyclopentanol, methylcyclopentanol, cyclohexanol.
9. The process according to claim 1, wherein the secondary alcohol is selected from one or more of isopropanol, sec-butanol, 2-pentanol, 3-pentanol.
10. The process according to claim 1, wherein the molar ratio of benzene to secondary alcohol is 1: (5-100), the molar ratio of benzene to hydrogen peroxide is 1: (0.1-5), wherein the weight ratio of the catalyst containing the catalytic active center of the oxidation reaction to benzene in the composite catalyst is (0.01-0.3): 1, the reaction temperature is 40-100 ℃.
11. The process according to claim 10, wherein the molar ratio of benzene to secondary alcohol is 1: (10-80); the molar ratio of benzene to hydrogen peroxide is 1: (0.8-4).
12. The process according to claim 11, wherein the molar ratio of benzene to secondary alcohol is 1: (20-50), the molar ratio of benzene to hydrogen peroxide is 1: (1.5-3).
13. The process according to claim 10, wherein the weight ratio of the catalyst containing the catalytic active sites for oxidation reaction to benzene in the composite catalyst is (0.05 to 0.2): 1.
14. the process according to claim 13, wherein the weight ratio of the catalyst containing the catalytic active sites for oxidation reaction to benzene in the composite catalyst is (0.07-0.15): 1.
15. the method according to claim 6, wherein the ratio of the number of moles of the oxidative catalytic active sites to the number of moles of the catalytic active sites of the MPV reaction is 1: (0.3-0.8).
16. The method of claim 15, wherein the ratio of the number of moles of oxidative catalytic active sites to the number of moles of catalytic active sites for MPV reaction is 1: (0.4-0.6).
17. The process according to claim 1, wherein the catalyst containing the catalytic active sites for MPV reaction in the composite catalyst is prepared by a process comprising the steps of contacting a molecular sieve N having skeleton hydroxyl vacancies with a polyhydroxy compound and separating to obtain a molecular sieve O, and then contacting the molecular sieve O with a liquid P containing a zirconium source and recovering the product.
CN202010747645.7A 2020-07-30 2020-07-30 Method for simultaneously preparing phenol and benzenediol Active CN114057549B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202010747645.7A CN114057549B (en) 2020-07-30 2020-07-30 Method for simultaneously preparing phenol and benzenediol

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202010747645.7A CN114057549B (en) 2020-07-30 2020-07-30 Method for simultaneously preparing phenol and benzenediol

Publications (2)

Publication Number Publication Date
CN114057549A CN114057549A (en) 2022-02-18
CN114057549B true CN114057549B (en) 2024-02-09

Family

ID=80226968

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202010747645.7A Active CN114057549B (en) 2020-07-30 2020-07-30 Method for simultaneously preparing phenol and benzenediol

Country Status (1)

Country Link
CN (1) CN114057549B (en)

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5399336A (en) * 1990-06-29 1995-03-21 Rhone-Poulenc Chimie Stannozeosilite/zirconozeosilite zeolites and catalytic hydroxylation of phenolics therewith
US5466869A (en) * 1994-10-31 1995-11-14 Hoechst Celanese Corporation Process for perparing 4-hydroxyacetophenone oxime
JPH08157404A (en) * 1994-12-07 1996-06-18 Mitsui Toatsu Chem Inc Production of aromatic hydroxy compound
CN103232327A (en) * 2013-05-07 2013-08-07 中国科学院山西煤炭化学研究所 Method for co-production of phenol and benzenediol by direct oxidation of benzene
CN104707648A (en) * 2013-12-16 2015-06-17 中国科学院大连化学物理研究所 Ionothermal post-synthesis for synthesis of functional heteroatomic molecular sieve
CN109261208A (en) * 2018-09-30 2019-01-25 陕西科技大学 A kind of V/Zr-MOF catalyst and preparation method thereof preparing phenol for the direct hydroxylating of benzene

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
TWI471299B (en) * 2012-10-04 2015-02-01 China Petrochemical Dev Corp Taipei Taiwan Hydroxylation of phenol

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5399336A (en) * 1990-06-29 1995-03-21 Rhone-Poulenc Chimie Stannozeosilite/zirconozeosilite zeolites and catalytic hydroxylation of phenolics therewith
US5466869A (en) * 1994-10-31 1995-11-14 Hoechst Celanese Corporation Process for perparing 4-hydroxyacetophenone oxime
JPH08157404A (en) * 1994-12-07 1996-06-18 Mitsui Toatsu Chem Inc Production of aromatic hydroxy compound
CN103232327A (en) * 2013-05-07 2013-08-07 中国科学院山西煤炭化学研究所 Method for co-production of phenol and benzenediol by direct oxidation of benzene
CN104707648A (en) * 2013-12-16 2015-06-17 中国科学院大连化学物理研究所 Ionothermal post-synthesis for synthesis of functional heteroatomic molecular sieve
CN109261208A (en) * 2018-09-30 2019-01-25 陕西科技大学 A kind of V/Zr-MOF catalyst and preparation method thereof preparing phenol for the direct hydroxylating of benzene

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
Stability studies of stationary phases from poly(methyltetradecylsiloxane) sorbed and immobilized onto metalized and unmodified silicas;AnizioM. Faria et al.;《J. Sep. Sci.》;第30卷;第1844 – 1851页 *
无机多孔材料的合成及其在环境催化领域的应用;王斓懿 等;《物理化学学报》;第33卷(第12期);第2359-2376页 *

Also Published As

Publication number Publication date
CN114057549A (en) 2022-02-18

Similar Documents

Publication Publication Date Title
KR100555100B1 (en) Crystalline mww-type titanosilicate, its preparation and use thereof for producing epoxides
US8932980B2 (en) Ordered mesoporous titanosilicate and the process for the preparation thereof
CN102205974B (en) Method for preparing titanium silicon molecular sieve
Ivanchikova et al. Mesoporous niobium-silicates prepared by evaporation-induced self-assembly as catalysts for selective oxidations with aqueous H2O2
CN101229510A (en) Synthesis and applications of silicate containing Bi
Xu et al. Hydrophobic aluminosilicate zeolites as highly efficient catalysts for the dehydration of alcohols
Hutchings et al. Epoxidation of allyl alcohol to glycidol using titanium silicalite TS-1: effect of the reaction conditions and catalyst acidity
CN106276944B (en) A kind of HTS and its synthetic method and application and a kind of method for hydroxylation of phenol
CN106745025A (en) A kind of synthetic method of the HTSs of TS 1
CN108187726B (en) Preparation and application of Al-SBA-15 mesoporous molecular sieve and fatty alcohol ethoxylation reaction method
CN102227416A (en) Method for producing phenolphthalein using heteropolyacid catalyst
CN102309981A (en) Hydrothermal regenerating method of titanium silicon molecular sieve
Sahu et al. Zeolite-β based molecular sieves: A potential catalyst for esterification of biomass derived model compound levulinic acid
CN102227415A (en) Catalytic method for producing phenolphthalein compounds
CN114057549B (en) Method for simultaneously preparing phenol and benzenediol
CN114057209B (en) Zirconium-containing heteroatom molecular sieve, preparation method and application thereof
Singh et al. Liquid phase oxidation reactions over chromium silicalite-1 (CrS-1) molecular sieves
Pan et al. Cu supported over Al-pillared interlayer clays catalysts for direct hydroxylation of benzene to phenol
CN114105158B (en) Tin titanium silicon molecular sieve and preparation method and application thereof
CN108722455B (en) Preparation method of vanadium phosphorus oxide catalyst
CN110170327B (en) Mesoporous C/SiO2Supported heteropolyacid catalyst and preparation method and application thereof
CN102259022B (en) Titanium-containing molecular sieve composite material and preparation method thereof
CN109721071B (en) Method for producing titanium-silicon molecular sieve, titanium-silicon molecular sieve produced by method and hydroxylation reaction method
CN113786837A (en) Method for preparing cyclopentanone and cyclopentanol through furfural hydrogenation rearrangement
CN110201716B (en) Alcohol amine group modified ordered mesoporous C/SiO2Supported heteropolyacid catalyst and preparation method and application thereof

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant