CN106966872A - A kind of aromatic oxidation process - Google Patents

A kind of aromatic oxidation process Download PDF

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Publication number
CN106966872A
CN106966872A CN201610019806.4A CN201610019806A CN106966872A CN 106966872 A CN106966872 A CN 106966872A CN 201610019806 A CN201610019806 A CN 201610019806A CN 106966872 A CN106966872 A CN 106966872A
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beds
titanium
hts
reaction
silicon
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CN106966872B (en
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林民
史春风
朱斌
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Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
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Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
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    • 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
    • B01J29/89—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

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention discloses a kind of aromatic oxidation process, this method is included under oxidation reaction condition, make containing at least one aromatic hydrocarbons, the reaction feed of oxidant and solvent flows successively through the 1st beds to the n-th last beds, n is more than 2 integer, at least one HTS is filled with the beds, during this method is additionally included in reaction feed by the 1st beds to the n-th beds, to the 1st beds to introducing at least one carrying object between at least one pair of adjacent beds between the n-th beds, so that on the basis of the flow direction of reaction feed, in this pair of adjacent beds, superficial velocity positioned at reaction stream in the beds in downstream is higher than the superficial velocity of the reaction stream in the beds of upstream.The method according to the invention can effectively extend the single trip use life-span of HTS, improve the effective rate of utilization and target product selectivity of oxidant.

Description

A kind of aromatic oxidation process
Technical field
The present invention relates to a kind of aromatic oxidation process.
Background technology
Phenolic compound is a kind of material for being widely present in nature and having important use in the industry.From In right boundary, widely known anthocyanidin, vanillic aldehyde and catechol is exactly polyphenol substance.In industrial circle, Aldehydes matter is the important intermediate for synthesizing many organic compounds, and in addition, aldehydes matter is acted also as The role for vital stain, dyestuff and medicine.The important function and extensive use of aldehydes matter are determined Its importance synthesized.The method for preparing phenolic compound conventional at present mainly has oxidation aromatic hydrocarbons reaction, The displacement hydrolysis of aryl thallium salt, halogeno-benzene hydrolysis and diazol method etc..Hydrolyzed using halogeno-benzene, it usually needs HTHP and catalyst presence could be carried out；And prepare phenols using diazol method, it is necessary to synthesis step It is rapid a lot；Although the reaction temperature that the displacement hydrolysis of aryl thallium salt needs is low, speed also quickly, is reacted In used poisonous heavy metal thallium compound, be not suitable for large-scale popularization.In view of above present situation, exploitation is new The method for rapidly and efficiently preparing phenolic compound, many problems in synthetic work can be solved.
Phenol is important large industrial chemicals product in current organic chemical industry, world demand amount in 2000 More than 66Mt, it is mainly used to prepare bisphenol-A, phenolic resin and pharmaceutical intermediate etc..In addition, Phenol and its derivatives are additionally operable to the production of paint, dyestuff, explosive, petroleum additive, timber preservative etc. In.Catalyst benzene oxidatoin is made with HTS and prepares phenol, reaction condition is gentle, technical process Simply, it is environment-friendly.But with the extension in reaction time, the catalytic activity of HTS can be in decline Trend, causes desirable oxidation selectivity of product substantially to reduce.When reaction is carried out in fixed bed reactors, Because titanium molecular sieve catalysis activity reduction is, it is necessary to which HTS is entered in reactor or outside reactor Row regeneration, causes reactor down-time, so as to influence production efficiency and improve the operating cost of device.
Aromatic hydrocarbons oxygen of the phenol reactant as representative is prepared for the benzene oxidatoin using HTS as catalyst For the method for changing phenolic compound processed, how to extend the single trip use life-span of catalyst, reduction regeneration frequency Rate is raising production efficiency and reduces one of key link of operating cost.
The content of the invention
It is an object of the invention to provide a kind of aromatic oxidation process, this method can extend the one way of catalyst Service life, also can be by feed stock conversion, oxidant effective rate of utilization and mesh even if continuous run in long period Mark oxidation product selectively stable in higher level.
To achieve these goals, the present invention provides a kind of aromatic oxidation process, and this method is included in oxidation Under reaction condition, enter the reaction containing at least one aromatic hydrocarbons, oxidant and optional at least one solvent Material flows successively through the 1st beds to the n-th last beds, and n is more than 2 integer, Be filled with least one HTS in each beds, it is characterised in that react into During material passes through the 1st beds to the n-th beds, urged to the 1st beds to n-th Introduce carrying object between at least one pair of adjacent beds between agent bed so that with react into On the basis of the flow direction of material, at least one pair of adjacent beds, the beds positioned at downstream The superficial velocity of middle reaction stream is higher than the superficial velocity of the reaction stream in the beds of upstream.
By above-mentioned technical proposal, method of the invention can effectively extend the single trip use of HTS In the life-span, the regeneration frequency of HTS is reduced, extend the terminal life of HTS.
Other features and advantages of the present invention will be described in detail in subsequent embodiment part.
Brief description of the drawings
Accompanying drawing is, for providing a further understanding of the present invention, and to constitute a part for specification, with Following embodiment is used to explain the present invention together, but is not construed as limiting the invention. In accompanying drawing：
Fig. 1 is the XRD spectra of the titanium-silicon molecular sieve TS-1 prepared by the embodiment of the present invention 1.
Embodiment
The embodiment of the present invention is described in detail below in conjunction with accompanying drawing.It should be appreciated that Embodiment described herein is merely to illustrate and explain the present invention, and is not limited to this hair It is bright.
The present invention provides a kind of aromatic oxidation process, and this method is included under oxidation reaction condition, make containing The reaction feed of at least one aromatic hydrocarbons, oxidant and optional at least one solvent flows successively through the 1st catalysis Agent bed is to the n-th last beds, and n is more than 2 integer, each beds In be filled with least one HTS.Herein, " at least one " represents one or more kinds of； It is " optional " to represent inessential, it can be understood as " with or without ", " including or not including ".
In the present invention, n is the integer between 2-50, is preferably selected from the integer between 2-20, more preferably Integer between 2-10, is further preferably selected from the integer between 2-5, such as 2.
In the present invention, statement " reaction feed flows successively through the 1st to the n-th last beds " refers to Be to constitute the reaction feed successively from the 1st beds to the n-th last beds Glide path, but this does not imply that the reaction feed does not have any alternatively to flow through the 1st to last N-th beds.In fact, starting since entry into the 1st beds, reaction feed is (such as For its composition or character) it can be changed because occurring arene oxidizing reaction etc., thus lose it It is used as the initial composition or character of reaction raw materials.In consideration of it, in order to meet those skilled in the art to reaction The conventional understanding of raw material, in the context of the present invention, typically enters the reaction for flowing through each beds Material is referred to as reaction mass.Moreover, when flowing through different beds, the reaction mass as Various factors (such as because react or introduce new material, such as carrying object) and change, lead The reaction mass (such as its composition or character) for causing to flow through different catalysts bed is typically also not With.The present invention pays close attention to superficial velocity of each reaction mass when flowing through its corresponding catalyst bed.
The method according to the invention, is additionally included in reaction feed and passes through the 1st beds to the n-th catalysis During agent bed, urged to the 1st beds at least one pair of between the n-th beds is adjacent Introduce carrying object between agent bed so that on the basis of the flow direction of reaction feed, this at least one pair of it is adjacent Beds in, in the beds in downstream the superficial velocity of reaction stream be higher than be located at it is upper The superficial velocity of reaction stream in the beds of trip.
In the present invention, the superficial velocity is (with kg/ (m2S) count) refer in the unit interval by certain The mass flow (in terms of kg/s) and the beds of the whole reaction mass of one beds are a certain Cross-sectional area is (with m2Meter) ratio.For example, flowing through the table of the reaction mass of the 1st beds Sight speed is v1, refer to the quality by the whole reaction mass of the 1st beds in the unit interval Flow (in terms of kg/s) is with a certain cross-sectional area of the beds (with m2Meter) ratio.Here, For the angle that the present invention is described is simplified, " cross-sectional area " is generally referred to as average traversal area. Moreover, so-called " average traversal area ", refers to the total catalyst admission space of the beds (with m3Meter) with the beds along reaction mass flow direction length (in terms of m) ratio, This is obvious to those skilled in the art.For isometrical beds, the average horizontal stroke Sectional area is cross-sectional area.In addition, of the invention to flowing through the apparent of the reaction mass of each beds Speed (absolute value) can directly be applicable those conventionally known in the art, such as without particular/special requirement The superficial velocity (absolute value) for flowing through the reaction mass of the 1st beds typically can be 0.001-200kg/(m2S) in the range of, but this is not limited to sometimes.
From making the technology of the present invention effect more excellent angle, urged to the 1st beds to n-th At least one carrying object is introduced between at least one pair of adjacent beds between agent bed so that On the basis of the flow direction of reaction feed, in the pair of adjacent beds, positioned at urging for downstream The superficial velocity of reaction stream is expressed as v in agent bedm, the reactant in the beds of upstream The superficial velocity of stream is expressed as vm-1, the introduction volume of the carrying object causes vm/vm-1=1.5-15, it is more excellent Select vm/vm-1=2-10, further preferred vm/vm-1=2-5, m are the arbitrary integer in [2, n] interval, I.e. selection 2,3 ..., any one integer in n；Also, as n=2, m=2.For example, During m=2, preferably v2/v1=1.5-15, more preferably v2/v1=2-10, further preferred v2/v1=2-5.
The method according to the invention, the 1st to the n-th beds can all be arranged at same In reactor, the differential responses region of the reactor is constituted, can also be each arranged in n reactor, Constitute the different reactors of n, or be arranged in the way of any combination it is two or more (at most For n-1) in reactor, constitute the combination of multi-reaction-area domain and multiple reactor.
The method according to the invention, the described 1st to the n-th last beds can continuously be connected, Thus formula beds are integrally formed, can also any pair or multipair adjacent catalyst bed wherein There is separated place between layer, thus constitute multisection type beds.The separated place can be reactor Inner space, one or more non-catalytics bed can be now set in the inner space as needed Layer (bed being for example made up of inactive filler described below) or inner member (such as fluid distributor, Beds supporting member, heat exchanger etc.) etc., progress thus is reacted to the arene oxidizing of the present invention More flexible regulation.
The method according to the invention, the described 1st to the n-th last beds along it is described react into The glide path of material is sequentially connected in series, and constitutes upstream-downstream relationship, wherein the 1st beds are located at most Upstream, the n-th beds are located at most downstream.Even so, the catalyst of a portion or whole Bed can spatially be arranged side by side, as long as ensuring the reaction feed successively flowing by wherein i.e. Can.
The method according to the invention, the 1st to the n-th beds can each contain one or many Individual beds.If containing multiple beds, can be between the multiple beds It is connected in series, or be connected in parallel, can also is the combination for being connected in series and being connected in parallel.For example, When the multiple beds are divided into multigroup, the beds in every group can be connected in series and / or be connected in parallel, can be to be connected in series and/or be connected in parallel between each group.
The method according to the invention, from the angle for being easy to the arene oxidizing reaction of the present invention to implement, institute State the preferred fixed bed of the 1st to the n-th beds.
The method according to the invention, in the 1st to the n-th beds, is each filled with least A kind of HTS.HTS is a class of a part of silicon atom in titanium atom substitution lattice framework The general name of zeolite, can use chemical formula xTiO2·SiO2Represent.The present invention is for titanium in HTS The content of atom is not particularly limited, and can be the conventional selection of this area.Specifically, x can be 0.0001-0.05, preferably 0.01-0.03, more preferably 0.015-0.025.
The HTS can be the common HTS with various topological structures, for example： The HTS can be selected from the HTS (such as TS-1) of MFI structure, MEL structures HTS (such as TS-2), the HTS (such as Ti-Beta) of BEA structures, MWW structures HTS (such as Ti-MCM-22), the HTS (such as Ti-MOR) of MOR structures, The HTS (such as Ti-TUN) of TUN structures, the HTS of two dimension hexagonal structure are (such as Ti-MCM-41, Ti-SBA-15) and other structures HTS (such as Ti-ZSM-48).Institute State HTS be preferably selected from the HTS of MFI structure, the HTS of MEL structures, The HTS of two-dimentional hexagonal structure and the HTS of BEA structures, more preferably MFI structure HTS, such as non-hollow titanium-silicon molecular sieve TS-1 and/or hollow titanium-silicon molecular sieve TS-1. The hollow titanium-silicon molecular sieve TS-1 is the HTS of MFI structure, the crystalline substance of the HTS Grain is hollow-core construction, and the radical length of the chamber portion of the hollow-core construction is 5-300 nanometers, and the titanium silicon Molecular sieve is in 25 DEG C, P/P0=0.10, adsorption time is the benzene adsorbance measured under conditions of 1 hour for extremely Few 70 milligrams per grams, between the adsorption isotherm and desorption isotherm of the nitrogen absorption under low temperature of the HTS There is hysteresis loop.The hollow titanium-silicon molecular sieve TS-1 is commercially available (such as commercially available from Hunan The trade mark for building feldspathization limited company is HTS molecular sieve), can also be according to CN1132699C Disclosed in method prepare.
The method according to the invention, at least part HTS is titanium-silicon molecular sieve TS-1, the titanium silicon The surface silicon titanium ratio of molecular sieve TS-1 is not less than body phase silicon titanium ratio, and so can further improve oxidant has Utilization rate is imitated, and can further extend the single trip use life-span of HTS.Preferably, the table Face silicon titanium than with the body phase silicon titanium than ratio be more than 1.2.It is highly preferred that the surface silicon titanium ratio With the body phase silicon titanium than ratio be 1.2-5.It is further preferred that the surface silicon titanium ratio with it is described Body phase silicon titanium than ratio be 1.5-4.5.It is further preferred that the surface silicon titanium ratio and the body phase Silicon titanium than ratio be 2-3.Mol ratio of the silicon titanium than referring to silica and titanium oxide, the surface Silicon titanium ratio is determined using X-ray photoelectron spectroscopy, and the body phase silicon titanium ratio uses XRF light Spectrometry is determined.
The method according to the invention, the titanium-silicon molecular sieve TS-1 is using the method system comprised the following steps It is standby：
(A) inorganic silicon source is dispersed in the aqueous solution containing titanium source and alkali source template, and alternatively Water is supplemented, is obtained in dispersion liquid, the dispersion liquid, silicon source：Titanium source：Alkali source template：Mole of water Than for 100：(0.5-8)：(5-30)：(100-2000), the inorganic silicon source is with SiO2Meter, the titanium Source is with TiO2Meter, the alkali source template (contains nitrogen member in terms of OH- or N in the alkali source template When plain, in terms of N；In the alkali source template not Nitrogen element, in terms of OH-)；
(B) alternatively, the dispersion liquid is stood into 6-24h at 15-60 DEG C；
(C) dispersion liquid that the dispersion liquid or step (B) obtained step (A) is obtained is anti-in sealing Stage (1) of sequentially being undergone in kettle, stage (2) and stage (3) is answered to carry out crystallization, the stage (1) exists 80-150 DEG C of crystallization 6-72 hours (h), the stage (2) is cooled to not higher than 70 DEG C and residence time at least After 0.5h, the stage (3) is warming up to 120-200 DEG C of crystallization 6-96h again.
The alkali source template can be various templates usually used during synthesis of titanium silicon molecular sieve Agent, for example：The alkali source template can be one kind in quaternary ammonium base, aliphatic amine and aliphatic hydramine Or it is two or more.The quaternary ammonium base can be various organic level Four ammonium alkali, and the aliphatic amine can be each Plant NH3In at least one hydrogen replaced by aliphatic alkyl (such as alkyl) after the compound that is formed, it is described Aliphatic hydramine can be various NH3In at least one hydrogen by aliphatic group (such as alkane of hydroxyl Base) compound that is formed after substitution.
Specifically, the fat that the alkali source template can represent for the quaternary ammonium base that is represented selected from Formulas I, Formula II It is more than one or both of aliphatic hydramine that fat race amine and formula III are represented.
In Formulas I, R1、R2、R3And R4Respectively C1-C4 alkyl, includes C1-C4 straight chain alkane The branched alkyl of base and C3-C4, R1、R2、R3And R4Instantiation can include but is not limited to first Base, ethyl, n-propyl, isopropyl, normal-butyl, sec-butyl, isobutyl group or the tert-butyl group.
R5(NH2)n(Formula II)
In Formula II, n is 1 or 2 integer.When n is 1, R5For C1-C6 alkyl, including C1-C6 Straight chained alkyl and C3-C6 branched alkyl, its instantiation can include but is not limited to methyl, ethyl, It is n-propyl, isopropyl, normal-butyl, sec-butyl, isobutyl group, the tert-butyl group, n-pentyl, neopentyl, different Amyl group, tertiary pentyl or n-hexyl.When n is 2, R5For C1-C6 alkylidene, including C1-C6's is straight The branched alkylidene of chain alkylidene and C3-C6, its instantiation can include but is not limited to methylene, Asia Ethyl, sub- n-propyl, sub- normal-butyl, sub- n-pentyl or sub- n-hexyl.
(HOR6)mNH(3-m)(formula III)
In formula III, m is 1,2 or 3.R6Can be C1-C4 alkylidene, including C1-C4's is straight The branched alkylidene of chain alkylidene and C3-C4, its instantiation can include but is not limited to methylene, Asia Ethyl, sub- n-propyl and sub- normal-butyl.
The instantiation of the alkali source template can include but is not limited to：TMAH, tetrem Base ammonium hydroxide, TPAOH (include the various isomers of TPAOH, such as four just Propyl group ammonium hydroxide and tetra isopropyl ammonium hydroxide), TBAH (including tetrabutylammonium hydroxide The various isomers of ammonium, such as 4-n-butyl ammonium hydroxide and four isobutyl group ammonium hydroxide), ethamine, positive third Amine, n-butylamine, di-n-propylamine, butanediamine, hexamethylene diamine, MEA, diethanol amine and triethanolamine One or both of more than.Preferably, the alkali source template is tetraethyl ammonium hydroxide, tetrapropyl It is more than one or both of ammonium hydroxide and TBAH.It is highly preferred that the alkali source template Agent is TPAOH.
The titanium source can be inorganic titanium salt and/or organic titanate, preferably organic titanate.It is described Inorganic titanium salt can be TiCl4、Ti(SO4)2Or TiOCl2One or both of more than；It is described organic Titanate esters can be general formula R7 4TiO4The compound of expression, wherein, R7For C1-C6 alkyl, preferably For C2-C4 alkyl.
The inorganic silicon source can be silica gel and/or Ludox, preferably silica gel.SiO in the Ludox2 Weight/mass percentage composition can be more than 10%, preferably more than 15%, more preferably more than 20%. When preparing according to the HTS of the preferred embodiment, without using organic silicon source, such as organosilan and Organosiloxane.
In the dispersion liquid, silicon source：Titanium source：Alkali source template：The mol ratio of water is preferably 100：(1-6)： (8-25)：(200-1500), more preferably 100：(2-5)：(10-20)：(400-1000).
The dispersion liquid that step (A) is obtained, which can be sent directly into step (C), carries out crystallization.Preferably, 6-24h is stood at a temperature of 15-60 DEG C in the dispersion liquid feeding step (B) that step (A) is obtained. Step (B) is carried out between step (A) and step (C) can significantly improve the titanium silicon point finally prepared Son sieve TS-1 surface silicon titanium ratio so that the surface silicon titanium ratio of the HTS finally prepared is not less than Body phase silicon titanium ratio, can so significantly improve the catalytic performance of the HTS finally prepared, extend its list Journey service life, and improve oxidant effective rate of utilization.Usually, by step (A) and step (C) setting steps (B) between, surface silicon titanium ratio and the body phase silicon titanium of the HTS finally prepared The ratio of ratio can be in the range of 1.2-5, (such as in 2.5-4.5 model preferably in the range of 1.5-4.5 In enclosing), more preferably in the range of 2-3.The standing is carried out more preferably at a temperature of 20-50 DEG C, As carried out at a temperature of 25-45 DEG C.
In step (B), when being stood, dispersion liquid can be placed in sealing container, can also It is placed in open container and is stood.Preferably, step (B) is carried out in sealing container, so may be used To avoid being introduced into foreign matter into dispersion liquid during standing or cause moieties in dispersion liquid to be waved Hair is lost in.
After the completion of step (B) described standing, directly the dispersion liquid through standing can be sent into reactor Crystallization is carried out, crystallization is carried out in feeding reactor after the dispersion liquid through standing can also being carried out into redisperse, It is preferred that sent into after redisperse in reactor, point for the dispersion liquid for carrying out crystallization so can be further improved Dissipate uniformity.The method of the redisperse can be conventional method, such as stirring, ultrasonically treated and vibration One or both of more than combination.The duration of the redisperse is can make the dispersion liquid through standing Form uniform dispersion liquid to be defined, typically can be 0.1-12h, such as 0.5-2h.The redisperse can be Carry out, carried out at a temperature of such as 15-40 DEG C under environment temperature.
In step (C), temperature is adjusted can root to the heating rate of each phase temperature and rate of temperature fall Selected, be not particularly limited according to the type of the crystallization device specifically used.In general, by temperature The heating rate that degree is increased to stage (1) crystallization temperature can be 0.1-20 DEG C/min, preferably 0.1-10 DEG C / min, more preferably 1-5 DEG C/min.Can by the rate of temperature fall of stage (1) temperature to stage (2) temperature Think 1-50 DEG C/min, preferably 2-20 DEG C/min, more preferably 5-10 DEG C/min.By stage (2) temperature Spend to stage (3) crystallization temperature heating rate can be 1-50 DEG C/min, preferably 2-40 DEG C/min, More preferably 5-20 DEG C/min.
In step (C), the crystallization temperature in stage (1) is preferably 110-140 DEG C, more preferably 120-140 DEG C, More preferably 130-140 DEG C.The crystallization time in stage (1) is preferably 6-24h, more preferably 6-8h. The temperature in stage (2) is preferably not higher than 50 DEG C.The residence time of (2) in stage is preferably at least 1h, More preferably 1-5h.The crystallization temperature in stage (3) is preferably 140-180 DEG C, more preferably 160-170 DEG C. The crystallization time in stage (3) is preferably 12-20h.
In step (C), in a preferred embodiment, the crystallization temperature in stage (1) is less than rank The crystallization temperature of section (3), so can further improve the catalytic performance of the HTS of preparation.It is excellent Selection of land, the crystallization temperature in stage (1) is lower 10-50 DEG C than the crystallization temperature in stage (3).It is highly preferred that The crystallization temperature in stage (1) is lower 20-40 DEG C than the crystallization temperature in stage (3).In step (C), In another preferred embodiment, the crystallization time in stage (1) is less than the crystallization time in stage (3), It so can further improve the catalytic performance of the HTS finally prepared.Preferably, stage (1) Crystallization time than the stage (3) the short 5-24h of crystallization time.It is highly preferred that the crystallization in stage (1) Time is than the short 6-12h of crystallization time in stage (3), such as short 6-8h.In step (C), both are excellent The embodiment of choosing be may be used alone, can also be used in combination, and preferred compositions are used, i.e. the stage (1) The requirement of both preferred embodiments is met simultaneously with the crystallization temperature and crystallization time in stage (3).
In step (C), another preferred embodiment in, the temperature in stage (2) is not higher than 50 DEG C, and the residence time is at least 0.5h, such as 0.5-6h, so can further improve the titanium finally prepared The catalytic performance of si molecular sieves.Preferably, the residence time in stage (2) is at least 1h, such as 1-5h. This preferred embodiment can preferred embodiment be used separately with foregoing two kinds, and can also combine makes With preferred compositions are used, i.e. the crystallization temperature and crystallization time and rank in stage (1) and stage (3) The temperature of section (2) and residence time meet the requirement of above-mentioned three kinds of preferred embodiments simultaneously.
HTS is reclaimed in the mixture that can be obtained using conventional method from step (C) crystallization. Specifically, will after the mixture that step (C) crystallization is obtained alternatively being filtered and washed Solid matter is dried and is calcined, so as to obtain HTS.The drying and the roasting can be with Carry out under normal conditions.Usually, the drying can be in environment temperature (such as 15 DEG C) to 200 DEG C At a temperature of carry out.The drying can be carried out under environmental pressure (generally 1 standard atmospheric pressure), It can also carry out at reduced pressure.The duration of the drying can be according to dry temperature and pressure Power and the mode of drying are selected, and are not particularly limited.For example, the drying is under ambient pressure During progress, temperature is preferably 80-150 DEG C, more preferably 100-120 DEG C, and the dry duration is preferred For 0.5-5h, more preferably 1-3h.The roasting can be carried out at a temperature of 300-800 DEG C, preferably Carry out, carried out more preferably at a temperature of 550-650 DEG C, further preferably at a temperature of 500-700 DEG C Carried out at a temperature of 550-600 DEG C.The duration of the roasting can be according to the temperature being calcined Selection, typically can be 2-12h, preferably 2-5h.The roasting is carried out preferably in air atmosphere.
The method according to the invention, at least part HTS is preferably modified HTS, this Sample can further lift the catalytic performance of HTS.The HTS of the modification refers to that experience changes Property processing HTS, in contrast, the HTS of modification is not undergone to be unmodified HTS.The modification comprises the following steps：Using as the HTS of raw material with containing Nitric acid (that is, HNO3) and at least one peroxide modification liquid contact.It is used as the titanium silicon point of raw material Son sieve refers to the HTS of the raw material as modification, can be without going through the modification HTS, or live through the modification but need and carry out again at the modification The HTS of reason.
Method according to the invention it is possible to which whole HTSs live through above-mentioned modification (i.e., HTS is modified HTS), or part HTS lives through above-mentioned change Property processing (that is, HTS is modified HTS and unmodified HTS).It is excellent Selection of land, on the basis of the total amount of HTS, at least more than 50 weight % HTS is to change Property HTS, more preferably at least more than 60 weight % HTS is modified titanium silicon point Son sieve, such as on the basis of the total amount of the HTS, the content of the HTS of the modification Can be 5-95 weight %, more preferably preferably 20-90 weight %, 40-80 weight %.
In the modification, peroxide can be selected from hydrogen peroxide, hydroperoxides and peracid.This In invention, hydroperoxides refer to that a hydrogen atom in hydrogen peroxide molecule is replaced and obtained by organic group The material arrived, peracid refers to the organic oxacid for containing-O-O- keys in molecular structure.
In the modification, the instantiation of the peroxide can include but is not limited to：Peroxide Change hydrogen, ethylbenzene hydroperoxide, TBHP, cumyl hydroperoxide, cyclohexyl hydroperoxide, Peracetic acid and Perpropionic Acid.Preferably, the oxidant is hydrogen peroxide.The hydrogen peroxide can be with For the hydrogen peroxide existed in a variety of manners commonly used in the art.
In the modification, the mol ratio of HTS and the peroxide as raw material can Think 1：(0.01-5), preferably 1：(0.05-3), more preferably 1：(0.1-2).The nitric acid Consumption can be selected according to the consumption of the peroxide.Usually, the peroxide with it is described The mol ratio of nitric acid can be 1：(0.01-50), preferably 1：(0.1-20), more preferably 1：(0.2-10), More preferably 1：(0.5-5), particularly preferably 1：(0.6-3.5), such as 1：(0.7-1.2), it is described HTS is in terms of silica.
In the modification liquid, the concentration of the peroxide and nitric acid can be each 0.1-50 weight %. From the angle of the catalytic performance for the HTS for further improving the modification finally prepared, it is preferably 0.5-25 weight %.It is highly preferred that in the modification liquid, the concentration of the peroxide and nitric acid is each For 5-15 weight %.
The solvent of the modification liquid various can simultaneously dissolve nitric acid and the peroxide to be common Solvent.Preferably, the solvent of the modification liquid is water.
, can be at 10-350 DEG C as the HTS and modification liquid of raw material in the modification At a temperature of contacted.From the catalytic performance of the HTS for further improving the modification finally prepared Angle is set out, and the contact is preferably contacted at a temperature of 20-300 DEG C.It is highly preferred that described connect Touch and carried out at a temperature of 50-250 DEG C.It is further preferred that the contact is at a temperature of 60-200 DEG C Carry out.It is further preferred that the contact is carried out at a temperature of 70-150 DEG C.The contact is held The continuous time can be 1-10h, preferably 3-5h.In the modification, the titanium silicon of raw material will be used as The pressure in container that molecular sieve is contacted with the modification liquid can be selected according to Contact Temperature, It can be environmental pressure, or pressurization.Usually, using as the HTS of raw material with it is described The pressure in container that modification liquid is contacted can be 0-5MPa, and the pressure is gauge pressure.Preferably, It will be contacted under pressure as the HTS of raw material with the modification liquid.It is highly preferred that In will be contacted under self-generated pressure as the HTS of raw material with the modification liquid in closed container.
In the modification, the exposure level as the HTS and the modification liquid of raw material is excellent Choosing causes, using on the basis of the HTS as raw material, in ultraviolet-visible spectrum, modified titanium The peak area reduction by more than 2% of absworption peak of the si molecular sieves between 230-310nm, modified titanium silicon point The pore volume of son sieve reduces more than 1%.Absworption peak of the modified HTS between 230-310nm Peak area preferably reduces 2-30%, more preferably reduces 2.5-15%, further preferably reduces 3-10%, more Further preferably reduction 3-6%.The pore volume of modified HTS preferably reduces 1-20%, more preferably 1.5-10% is reduced, 2-5% is further preferably reduced.The pore volume is using static determination of nitrogen adsorption.
In the various commercial plants using HTS as catalyst, such as Ammoximation reaction and epoxy Change in reaction unit, generally plant running for a period of time after, the catalytic activity of catalyst declines, and needs Carry out in device or ex-situ regeneration, even if when carrying out regeneration and also being difficult to obtain satisfied activity, it is necessary to will Catalyst is drawn off (that is, more catalyst changeout) from device, and draw off catalyst (that is, draw off agent or Dead catalyst) current processing method be typically accumulation bury, on the one hand occupy preciousness land resource And inventory space, another aspect HTS production cost is higher, directly passes into disuse and also result in pole Big waste.By these draw off after agent (that is, the HTS drawn off) is regenerated with aromatic hydrocarbons and oxygen Agent is contacted under oxidation reaction condition, remains able to obtain preferable catalytic performance, can particularly be obtained Higher oxidant effective rate of utilization.Therefore, the method according to the invention, at least partly described titanium silicon point Son sieve is preferably the reaction unit using HTS as catalyst through regeneration (except arene oxidizing reaction Outside device) draw off agent.It is described draw off agent can be to use HTS as catalyst from various What is drawn off in reaction unit draws off agent, for example, can draw off agent for what is drawn off from oxidation reaction apparatus.Tool Body, it is described to draw off agent and draw off drawing off for agent and/or epoxidation reaction device for Ammoximation reaction device Agent.Draw off agent more specifically, described and can draw off agent and/or propylene for cyclohexanone oxamidinating reaction unit Epoxidation reaction device draws off agent.
The condition that agent regenerated will be drawn off to be not particularly limited, can be fitted according to the source for drawing off agent When selection, for example：High-temperature roasting and/or solvent washing.
The activity for drawing off agent through regeneration is different according to its source.Usually, drawing off through regeneration The activity (that is, the activity of fresh HTS) that the activity of agent can be the HTS when fresh 5-95%.Preferably, the activity for drawing off agent through regeneration can be the HTS when fresh The 10-90% of activity, the more preferably active 30-50% when fresh, still more preferably for Active 35-45% when fresh.The activity of the fresh HTS is generally more than 90%, Usually more than 95%.
The activity is determined by the following method：Agent and fresh HTS will be drawn off through regeneration respectively The catalyst reacted as cyclohexanone oxamidinating, the condition of the Ammoximation reaction is：HTS, 36 Weight % ammoniacal liquor is (with NH3Meter), 30 weight % hydrogen peroxide is (with H2O2Meter), the tert-butyl alcohol and ring Hexanone is by weight 1：7.5：10：7.5：10, react 2h in 80 DEG C at atmosheric pressure.Count respectively Calculate using the conversion ratio of cyclohexanone when drawing off agent and fresh HTS as catalyst through regeneration, and by its Respectively as the activity for drawing off agent and fresh HTS through regeneration, wherein, the conversion ratio of cyclohexanone Cyclohexanone that=[(mole of the mole of the cyclohexanone of addition-unreacted cyclohexanone)/adds rubs You measure] × 100%.
The method according to the invention, it is described to draw off the raw material that agent be modified HTS, also may be used To be used as unmodified HTS.Preferably, in the modification, it is used as the titanium of raw material Si molecular sieves draw off agent to be described, so can further extend the single trip use life-span, and with it is non-modified The agent that draws off compare, the selectivity and aromatics conversion rate of phenol can be significantly improved.
The method according to the invention, the 1st to the n-th beds are each filled with before at least one The HTS stated.The species of the HTS loaded in different catalysts bed can be identical, Can also be difference.Also, a kind of foregoing titanium silicon point can also be only loaded in each beds Son sieve, can also load one or more kinds of foregoing titanium silicon molecules according to the relative scale arbitrarily needed Sieve.
Preferably, the HTS of the 1st beds filling is hollow HTS TS-1, the 2nd to the n-th beds (that is, residual catalyst bed) filling HTS be HTS in addition to hollow titanium-silicon molecular sieve TS-1, the titanium silicon point such as selected from other MFI structures Son sieve, so can further delay the deactivation rate of HTS.It is highly preferred that the described 1st urges The HTS of agent bed filling is hollow titanium-silicon molecular sieve TS-1, the 2nd to the n-th catalyst The HTS of bed filling is non-hollow titanium-silicon molecular sieve TS-1.So can not only further it prolong The deactivation rate of slow HTS, extends the single trip use life-span of HTS, and can also enter one Step improves desirable oxidation selectivity of product.Herein, as do not specialized " hollow HTS TS-1 ", then be defaulted as non-hollow titanium-silicon molecular sieve TS-1.
The method according to the invention, foregoing HTS is preferably shaping HTS.It is molded titanium Si molecular sieves typically contain the HTS as active component and the carrier as binding agent, wherein, The content of HTS can be conventional selection.Usually, with the total amount of the shaping HTS On the basis of, the content of HTS can be 5-95 weight %, preferably 10-95 weight %, more excellent Elect 70-90 weight % as；The content of the carrier can be 5-95 weight %, preferably 5-90 weight %, More preferably 10-30 weight %.The carrier of the shaping HTS can be conventional selection, such as oxygen Change aluminium and/or silica.The method for preparing the shaping HTS is it is known in the art, herein No longer it is described in detail.The granular size of the shaping HTS is also not particularly limited, can be according to specific Shape carries out appropriate selection.Usually, the average grain diameter of the shaping HTS can be 4-10000 microns, preferably 5-5000 microns, more preferably 40-4000 microns, such as 100-2000 is micro- Rice.The average grain diameter is volume average particle size, can be determined using laser particle analyzer.
The titanium silicon molecule each loaded in the method according to the invention, the 1st to the n-th beds The amount (quality) of sieve can be identical, or different.According to a kind of embodiment, m takes interval During arbitrary integer in [2, n], Wm-1/WmFor 0.1-20, Wm-1/WmPreferably more than 0.5, it is more excellent Elect more than 1, more preferably more than 2 as.Here, Wm-1It is the 1st beds to last Filled in n-th beds in any pair of adjacent beds in the beds of upstream The quality for the catalyst filled out, WmFor the 1st beds into the n-th beds any pair of phase It is located at the quality of the catalyst loaded in the beds in downstream in adjacent beds.Wm-1/Wm Preferably less than 15, more preferably less than 10.It is further preferred that Wm-1/WmFor 2-8.Wm-1 And WmThe content of HTS is determined in the shaping HTS.In addition, each catalyst The amount of the catalyst loaded in bed (can such as produce capacity) as needed and rationally determine, not have herein There is special restriction.
The method according to the invention, total amount (that is, described 1st to the n-th catalyst bed of HTS The total amount of the titanium-silicon molecular sieve catalyst loaded in layer) it can be selected according to the specific treating capacity of system Select.Usually, the total amount of the catalyst causes the weight of aromatic hydrocarbons (as the component of the reaction feed) When air speed can be 0.05-100h-1, preferably 0.1-50h-1。
Except loading the titanium silicon point in the method according to the invention, the 1st to the n-th beds Outside son sieve, inactive filler can also be further loaded as needed.Can be the whole the described 1st The inactive filler is loaded into the n-th beds, can also be in the described 1st to the n-th catalysis The inactive filler is loaded in one or more of agent bed.Loaded in beds nonactive Filler can be adjusted to the amount of catalyst in beds, so that the speed to reaction is adjusted Section.For some beds, when loading inactive filler, the inactive filler Content can be 5-95 weight %, relative to the catalyst and inactive filler loaded in the beds Total amount for.Here, the inactive filler refers to no to arene oxidizing reaction or not urged substantially Change the filler of activity, conventionally known in this area, its instantiation can include but is not limited to：Stone It is more than one or both of sand, ceramic ring and potsherd.
According to the present invention, the reaction feed (refers in particular to that the 1st beds will be entered in the present invention Reaction mass before) contain at least one aromatic hydrocarbons, oxidant and optional solvent.
The oxidant can for it is conventional it is various can be by the material of arene oxidizing.Preferably, the oxygen Agent is peroxide, can be selected from hydrogen peroxide, hydroperoxides and peracid.The peroxide Instantiation can include but is not limited to：Hydrogen peroxide, TBHP, dicumyl peroxide, Ethylbenzene hydroperoxide, cyclohexyl hydroperoxide, Peracetic acid and Perpropionic Acid.Preferably, the oxidation Agent is hydrogen peroxide, so can further reduce separation costs.The hydrogen peroxide can be this area The conventional hydrogen peroxide existed in a variety of manners.The oxidant individually one kind can be used, can also Two or more is applied in combination.
The amount for the aromatic hydrocarbons that the consumption of the oxidant can be included according to the reaction feed is selected.One As, in the reaction feed, the mol ratio of the aromatic hydrocarbons and the oxidant can be (0.1-20)： 1.From the angle of the further selectivity for improving phenol, the mol ratio of the aromatic hydrocarbons and the oxidant Preferably (0.2-10)：1, more preferably (1-5)：1.
The method according to the invention, the reaction feed can also further contain solvent, so as to preferably Control reaction speed.The present invention is not particularly limited for the species of the solvent, and the solvent can be The various solvents commonly used in arene oxidizing reaction.Preferably, the solvent be water, C1-C10 alcohol, At least one of carboxylic acid of C3-C10 ketone, C2-C10 nitrile and C1-C6.Preferably, it is described molten Agent is more than one or both of C1-C6 nitrile of alcohol, C3-C8 ketone and C2-C5.It is highly preferred that The solvent is in methanol, ethanol, acetonitrile, normal propyl alcohol, isopropanol, the tert-butyl alcohol, isobutanol and acetone One or more.It is further preferred that the solvent is methanol, acetonitrile, acetone and the tert-butyl alcohol One or both of more than.These solvents individually one kind can be used, can also combination of two or more Use.
The present invention is not particularly limited for the consumption of the solvent, can be according to the amount of aromatic hydrocarbons and oxidant Selected.Usually, in the reaction feed, the mol ratio of the solvent and the aromatic hydrocarbons can be with For (0.1-100)：1, be preferably (0.2-80)：1.
The method according to the invention, when the condition of the oxidation reaction is enough arene oxidizing turning into phenol, this The method of invention is preferably also included to sending at least one alkaline matter in the liquid mixture, described The addition of alkaline matter causes the liquid mixture pH value to be in the range of 6-9, so can Further improve the selectivity of phenol.It is highly preferred that the addition of the alkaline matter causes the liquid to mix The pH value of compound is in the range of 6.5-8.5.
The method according to the invention, the aromatic hydrocarbons can be substituted or non-substituted mononuclear aromatics, can also For substituted or non-substituted polycyclic aromatic hydrocarbon, the substituent can be selected from alkyl, methoxyl group, alkyl halide At least one of base, preferably substituted or non-substituted mononuclear aromatics.These aromatic hydrocarbons can be individually a kind of Use, can also combination of two or more use.Specifically, the aromatic hydrocarbons can be selected from benzene, toluene, At least one of dimethylbenzene, ethylbenzene, isopropylbenzene.
Oxidation reaction condition in the method according to the invention, each beds can be with identical, can also Different (preferably identical), can each include：Reaction pressure (in terms of gauge pressure) is 0-3MPa, preferably 0.1-2.5MPa, reaction temperature is 0-120 DEG C, preferably 20-80 DEG C (such as 30-60 DEG C).
The method according to the invention, passes through the aromatic hydrocarbons oxygen carried out in the 1st to the n-th beds Change reaction, obtain the reaction discharging containing phenol.Here, the reaction discharging refers in particular to just leave described n-th Reaction mass after beds.
The method according to the invention, it is alternatively described including being isolated from the reaction discharging as needed Phenol, the step of obtaining off-gas stream.Here, the off-gas stream can be without further separation The mixture containing unreacted reactant, byproduct of reaction and solvent is rendered as, can also be passed through into one The separation of step and as single unreacted reactant, byproduct of reaction and solvent, these can be straight Connect and used as off-gas stream without any purification processes.As separation method, can directly it fit With in this area for this purpose it is conventional use of those, there is no particular limitation.Moreover, isolate Unreacted reactant and solvent can be recycled as a part for reaction feed.
The method according to the invention, by into the 1st to the n-th beds any pair or many Carrying object is introduced to the separated place (as previously described) between adjacent beds, place is flowed through to increase , can be thus corresponding in the overall circulation of the reaction mass of whole beds in the separated place downstream Increase the superficial velocity of each reaction mass, to meet the foregoing regulation of the present invention.For example, when n is 2, By introducing carrying object, Ke Yizeng to the separated place between the 1st beds and the 2nd beds Plus the overall circulation of the reaction mass of the 2nd beds is flowed through, thus accordingly increase by the 2nd catalysis The superficial velocity of reaction mass in agent bed, to meet the foregoing regulation of the present invention.
There is no particular limitation for introduction volume and incorporation way of the present invention to the carrying object, as long as it can (1) with the reaction mass come out from the beds in the separated place immediately upstream, entering Before beds in the direct downstream in the separated place, during or after, be well mixed, and And (2) cause the superficial velocity of each reaction mass to meet the foregoing regulation of the present invention.
The method according to the invention, the carrying object can be solvent, non-active gas and catalyst bed Combination more than one or both of effluent of layer.The effluent of the bed of the catalyst refer to from A beds or multiple beds outflow of 1st catalyst into the n-th beds The effluent of the beds of effluent, preferably most downstream.The effluent of beds can not Use, used after target phenol can also be isolated as carrying object directly as carrying object through separating.According to The method of the present invention, the carrying object is more preferably separated from the effluent of the beds of most downstream Go out remaining logistics after target oxide, such as previously described off-gas stream.
Fluid distributor etc. can be set in the separated place by any mode known in the art, Thus the uniform introducing of carrying object is conducive to.As needed, it is described to carry before the separated place is introduced Fluid can be by pretreatments such as heat exchange (such as cooling) or pressurizations.
Describe the present invention in detail with reference to embodiments, but and be not so limited the scope of the present invention.
In following examples and comparative example, used reagent is commercially available reagent, and pressure is gauge pressure.
In following examples and comparative example, each composition in the reaction solution obtained using gas chromatography analysis Content, be respectively adopted on this basis below equation calculate aromatics conversion rate, oxidant effective rate of utilization with And phenol selectivity：
Aromatics conversion rate (%)=[(mole of the mole of the aromatic hydrocarbons of addition-unreacted aromatic hydrocarbons) The mole of/the aromatic hydrocarbons added] × 100%；
Oxidant effective rate of utilization=[mole/(mole of the oxidant of addition of the phenol of reaction generation The mole of-unreacted oxidant)] × 100%；
Phenol selectivity=[mole/(mole of the aromatic hydrocarbons of addition-unreacted of the phenol of reaction generation Aromatic hydrocarbons mole)] × 100%.
In following examples and comparative example, static nitrogen adsorption method is respectively adopted and solid ultraviolet-visible is unrestrained anti- Spectroscopic methodology is penetrated to characterize the pore volume and ultraviolet absorption peak of the HTS after before modified.Wherein, it is quiet State N2 adsorption is carried out on the static n2 absorption apparatus of the types of ASAP 2405 of Micromeritics companies, according to ASTM D4222-98 standard methods are measured.The nitrogen adsorption in liquid nitrogen cold trap, by titanium silicon molecule Sieve sample keeps 4h to be de-gassed under 393K, 1.3kPa vacuum, and nitrogen suction is carried out in 77K It is attached.Solid ultraviolet-visible diffusing reflection spectrum (UV-Vis) analysis is purple in SHIMADZU UV-3100 types Carry out, determined under normal temperature and pressure, scanning wavelength scope 190nm~800nm in outside-visible spectrophotometer. With powder pressing method, after sample calcination process, a certain amount of sample is taken, mortar grinder is put into and arrives<300 mesh, Tabletting sample preparation.
It is related to drawing off in the embodiment and comparative example of agent through regeneration below, titanium silicon is determined using following methods The activity of molecular sieve (including regenerative agent and fresh dose)：
By HTS, 36 weight % ammoniacal liquor (with NH3Meter), 30 weight % hydrogen peroxide (with H2O2Meter), the tert-butyl alcohol and cyclohexanone be by weight=1：7.5：10：7.5：In atmospheric pressure after 10 mixing In after 80 DEG C of stirring reactions 2 hours under power, reactant is filtered, liquid phase analyzed with gas-chromatography, The conversion ratio of cyclohexanone is calculated and as the activity of HTS using below equation,
The conversion ratio of cyclohexanone=[(mole of the cyclohexanone of addition-unreacted cyclohexanone mole) The mole of/the cyclohexanone added] × 100%.
In embodiment and comparative example included below the step of prepare HTS, X-ray diffraction analysis Carried out on Siemens D5005 type X-ray diffractometers, using sample and authentic specimen in 2 θ as 22.5 ° The ratio of diffracted intensity (peak height) sum at the five fingers diffractive features peak represents that sample is relative between -25.0 ° In the crystallinity of authentic specimen, test condition：CuK α are radiated, 44 kilovolts, 40 milliamperes, sweep speed For 2 °/minute.Fourier turn infrared is in the type Fourier infrared spectrographs of Nicolet 8210 Upper to carry out, KBr tablettings, infrared photometer resolution ratio is 4cm-1, test scope 400cm-1~4000 cm-1, scanning accumulative frequency 20 times.Mol ratio of the silicon titanium than referring to silica and titanium oxide, surface silicon titanium Than being determined using x-ray photoelectron spectroscopy, INSTRUMENT MODEL PHI Quantera SXM (Scanning X-ray Microprobe), using monochromator, from Al plate targets, energy resolution 0.5eV is sensitive Spend 3M CPS, 45 ° of incidence angle, analysis room's vacuum 6.7 × 10-8Pa；Body phase silicon titanium ratio is using Japan Rigaku Denki Co., Ltd 3271E types Xray fluorescence spectrometer is determined, rhodium target, excitation voltage 50kV, Excitation current 50mA, with scintillation counter and proportional counter detection each element the intensity of spectral line, uses powder After pressed disc method, sample calcination process, a certain amount of sample is taken, mortar grinder is put into and arrives<300 mesh, tabletting Sample preparation.
Embodiment 1-20 is used for the method for illustrating the present invention.
Embodiment 1
The catalyst used in the present embodiment is titanium-silicon molecular sieve TS-1, with reference to Zeolites, 1992, Vol.12 Prepared by the method described in the 943-950 pages, specific method is as follows.
At room temperature (20 DEG C), using 22.5g tetraethyl orthosilicates and 7.0g as template tetrapropyl Ammonium hydroxide is mixed, and adds 59.8g distilled water, and stirring mixing hydrolyzes 1.0h after normal pressure and 60 DEG C, Obtain the hydrating solution of tetraethyl orthosilicate.With vigorous stirring, slowly add into the hydrating solution Enter the solution being made up of 1.1g butyl titanates and 5.0g anhydrous isopropyl alcohols, by gained mixture at 75 DEG C 3h is stirred, clear colloid is obtained.This colloid is placed in stainless steel sealing reactor, at 170 DEG C At a temperature of constant temperature place 36h, obtain the mixture of crystallization product.By the filtering of obtained mixture, receive Collect after obtained solid matter water used wash, in 110 DEG C of dry 60min, be then calcined 6h at 500 DEG C, Titanium-silicon molecular sieve TS-1 is obtained, its titanium oxide content is 2.8 weight %.Its X-ray diffraction spectrogram (XRD Figure) as shown in figure 1, what is obtained is the TS-1 molecular sieves with MFI structure.By titanium silicon molecule The former powder of sieve TS-1 is mixed with Ludox, pore-foaming agent (APES) and starch, using crowded Bar machine carries out extrusion, then prepares the HTS that particle diameter is 500 microns through pelletizing, drying and roasting (wherein, 85%) weight/mass percentage composition of HTS is to TS-1 catalyst.
By Catalyst packing in draw ratio in 20 isometrical fixed bed reactors, to form beds, Wherein, the quantity of beds is 2 layers, and 2 layers of beds are arranged in parallel, spacing 10cm；Two Identical in quality, the respectively 200g of the catalyst loaded in individual beds；In two layers of beds Between carrying object entrance and liquid distributor are set, liquid distributor is used to be sent into by carrying object entrance Carrying object be well mixed with the effluent of first beds after, send into second beds In.
Using benzene, as oxidant hydrogen peroxide (in the form of 30 weight % hydrogen peroxide provide) and Reaction raw materials are mixed to form as the methanol of solvent, ammoniacal liquor is added into reaction raw materials, and (concentration is 25 weights Measure %), the pH value of reaction raw materials is adjusted to 6.8, reaction raw materials are sent into fixed bed reaction from bottom In device and flow through beds, with HTS haptoreaction.Wherein, benzene and hydrogen peroxide Mol ratio is 1：1, the mol ratio of benzene and methanol is 1：16.Temperature in reactor is 30 DEG C, reaction During by the Stress control in fixed bed reactors be 0.5MPa, the weight (hourly) space velocity (WHSV) of benzene is 5h-1。
The reactant mixture exported from reactor is flashed, gas stream and liquids is separated into Stream.Wherein, gas stream condenses benzene by cooling, to reclaim benzene；Liquid stream is distilled, point Not Shou Ji methanol, water and phenol, phenol is exported.It is heated to after the benzene and methanol of recovery are well mixed 30 DEG C sent between first beds and the second beds as carrying object, and carrying object is sent Enter amount so that v2/v1=2, v1For the superficial velocity of reaction stream in first beds, v2For The superficial velocity of reaction stream in two beds.
The reaction exported from second fixed bed reactors is monitored in course of reaction using gas-chromatography to mix The composition of compound, and calculate benzene conversion ratio, oxidant effective rate of utilization and phenol selectivity, reaction result Listed in table 1.
Embodiment 2
Using method same as Example 1 by benzene oxidatoin, unlike, the HTS used TS-1 is prepared using following methods.
First butyl titanate is dissolved in the alkali source template TPAOH aqueous solution, silicon is then added Glue (is purchased from Qingdao silica gel factory), obtains dispersion liquid, in the dispersion liquid, silicon source：Titanium source：Alkali source template Agent：The mol ratio of water is 100：4：12：400, silicon source is with SiO2Meter, titanium source is with TiO2Meter, alkali Source template is in terms of N.By above-mentioned dispersion liquid in beaker using sealed membrane sealing after room temperature (be 25 DEG C, 24h similarly hereinafter) is stood, 2h is stirred at 35 DEG C followed by magnetic agitation, is allowed to disperse again.Will again Dispersion liquid after scattered is transferred in sealing reactor, undergoes first stage crystallization 6h at 140 DEG C, then Mixture is cooled into 30 DEG C of experience second stage to stop after 2h, continued in sealing reactor in 170 DEG C At a temperature of undergo phase III crystallization 12h (wherein, by room temperature to first stage crystallization temperature Heating rate is 2 DEG C/min, by the rate of temperature fall of first stage crystallization temperature to second stage treatment temperature It it is 10 DEG C by the heating rate of second stage treatment temperature to phase III crystallization temperature for 5 DEG C/min / min), without filtering and washing step after gained crystallization product is taken out, 2h directly is dried in 110 DEG C, Then 3h is calcined at 550 DEG C, obtains molecular sieve.The XRD crystalline phases figure of gained sample is made with embodiment 1 Standby titanium-silicon molecular sieve TS-1 is consistent, and illustrate to obtain is the titanium-silicon molecular sieve TS-1 with MFI structure； In FFIR figure, in 960cm-1Nearby there is absworption peak, show that titanium has been enter into molecule In sieve skeleton frame, the HTS, titanium oxide content is 3.5 weight %, surface silicon titanium ratio/body phase silicon titanium Than (in HTS prepared by embodiment 1,1.05) surface silicon titanium ratio/body phase silicon titanium ratio is for 2.58. By the former powder of obtained titanium-silicon molecular sieve TS-1 and Ludox, pore-foaming agent (APES) and Starch is mixed, and extrusion is carried out using banded extruder, then it is 500 to prepare particle diameter through pelletizing, drying and roasting (wherein, 85%) weight/mass percentage composition of HTS is to the titanium-silicon molecular sieve TS-1 catalyst of micron.
Reaction result is listed in table 1.
Embodiment 3
Using method same as Example 2 by benzene, unlike, preparing titanium-silicon molecular sieve TS-1 When, the crystallization temperature of phase III is also 140 DEG C.The XRD crystalline phases figure of gained sample and embodiment 1 The titanium-silicon molecular sieve TS-1 of preparation is consistent, and illustrate to obtain is the TS-1 molecular sieves with MFI structure； In 960cm in fourier-transform infrared spectrogram-1Nearby there is absworption peak, show that titanium has been enter into molecule sieve skeleton In frame, the HTS, surface silicon titanium ratio/body phase silicon titanium ratio is 4.21, and titanium oxide content is 3.1 weights Measure %.Reaction result is listed in table 1.
Embodiment 4
Using method same as Example 2 by benzene oxidatoin, unlike, preparing HTS During TS-1, the crystallization temperature of first stage is 110 DEG C.The XRD crystalline phases figure and embodiment of gained sample 1 titanium-silicon molecular sieve TS-1 prepared is consistent, and illustrate to obtain is the TS-1 molecular sieves with MFI structure； In 960cm in fourier-transform infrared spectrogram-1Nearby there is absworption peak, show that titanium has been enter into molecule sieve skeleton In frame, the HTS, surface silicon titanium ratio/body phase silicon titanium ratio is 2.37, and titanium oxide content is 3.2 weights Measure %.Reaction result is listed in table 1.
Embodiment 5
Using method same as Example 2 by benzene oxidatoin, unlike, prepare titanium-silicon molecular sieve TS-1 When, the crystallization time of first stage is 12h.The XRD crystalline phases figure of gained sample is prepared with embodiment 1 Titanium-silicon molecular sieve TS-1 it is consistent, illustrate to obtain is the TS-1 molecular sieves with MFI structure；Fourier In 960cm in leaf transformation infrared spectrum-1Nearby there is absworption peak, show that titanium has been enter into framework of molecular sieve, In the HTS, surface silicon titanium ratio/body phase silicon titanium ratio is 3.78, and titanium oxide content is 3.4 weight %. Reaction result is listed in table 1.
Embodiment 6
Using method same as Example 2 by benzene oxidatoin, unlike, prepare titanium-silicon molecular sieve TS-1 When, second stage is to be cooled to 70 DEG C of stop 2h.The XRD crystalline phases figure of gained sample is made with embodiment 1 Standby titanium-silicon molecular sieve TS-1 is consistent, and illustrate to obtain is the TS-1 molecular sieves with MFI structure；Fu In 960cm in vertical leaf transformation infrared spectrum-1Nearby there is absworption peak, show that titanium has been enter into framework of molecular sieve, In the HTS, surface silicon titanium ratio/body phase silicon titanium ratio is 2.75, and titanium oxide content is 3.1 weight %. Reaction result is listed in table 1.
Embodiment 7
Using method same as Example 2 by benzene oxidatoin, unlike, aqueous dispersions are not at room temperature 24h is stood, but is sent directly into reactor and carries out crystallization.The XRD crystalline phases figure and reality of gained sample The titanium-silicon molecular sieve TS-1 for applying the step of example 1 (1) preparation is consistent, and illustrate to obtain is with MFI structure Titanium-silicon molecular sieve TS-1；In FFIR figure, in 960cm-1Nearby there is absworption peak, Show that titanium has been enter into framework of molecular sieve, in the HTS, titanium oxide content is 3.5 weight %, table Face silicon titanium ratio/body phase silicon titanium ratio is 1.18.Reaction result is listed in table 1.
Embodiment 8
Using method same as Example 1 by benzene oxidatoin, unlike, titanium-silicon molecular sieve TS-1 exists As being modified processing using following methods before catalyst.
Titanium-silicon molecular sieve TS-1 prepared by step (1) is with containing HNO3(HNO3Mass concentration Mixed for the aqueous solution 10%) with hydrogen peroxide (mass concentration of hydrogen peroxide is 7.5%), will To mixture in closed container in 70 DEG C of stirring reaction 5h, the temperature of obtained reactant mixture drops Filtered after to room temperature, obtained solid matter is dried to constant weight at 120 DEG C, modified titanium is obtained Si molecular sieves.Wherein, titanium-silicon molecular sieve TS-1 is with SiO2Meter, HTS and hydrogen peroxide rub You are than being 1：0.1.Compared with raw material HTS, the UV-Vis of the HTS of obtained modification The peak area of absworption peak in spectrum between 230-310nm reduces 3.5%, is surveyed by static nitrogen adsorption method Fixed pore volume reduces 2.6%.Reaction result is listed in table 1.
Embodiment 9
Using method same as Example 8 by benzene oxidatoin, unlike, in modification, it is used as original What is expected is titanium-silicon molecular sieve TS-1 (titanium silicon of being drawn off from cyclohexanone oxamidinating reaction unit through regeneration Molecular sieve TS-1 is prepared using method same as Example 1, and the titanium-silicon molecular sieve TS-1 drawn off exists 5h being calcined in air atmosphere at a temperature of 570 DEG C and being regenerated, the activity after regeneration is 35%, when fresh Activity for 96%).Compared with raw material HTS, the UV-Vis of the HTS of obtained modification The peak area of absworption peak in spectrum between 230-310nm reduces 3.3%, is surveyed by static nitrogen adsorption method Fixed pore volume reduces 2.8%.Reaction result is listed in table 1.
Embodiment 10
Using method same as Example 9 by benzene oxidatoin, unlike, original will be used as in embodiment 9 The titanium-silicon molecular sieve TS-1 drawn off from cyclohexanone oxamidinating reaction unit through regeneration of material is as catalysis Agent.Reaction result is listed in table 1.
Comparative example 1
Using method same as Example 1 by benzene oxidatoin, unlike, not in first catalyst bed Carrying object is introduced between layer and second beds.Reaction result is listed in table 1.
Table 1
Embodiment 11
The present embodiment is as the trade mark for being available from Hunan Jianchang Petrochemical Co., Ltd of catalyst HTS hollow TS-1 HTSs, its titanium oxide content is 2.5 weight %.
By Catalyst packing in draw ratio in 15 isometrical fixed bed reactors, to form beds, Wherein, the quantity of beds is 2 layers, and 2 layers of beds are arranged in parallel, spacing 15cm；The The weight ratio of the loadings of one beds and second beds is 2：1, respectively 500g And 250g.Carrying object entrance and liquid distributor, liquid distribution are set between two layers of beds Device is used to the effluent of first beds mix the carrying object sent into by carrying object entrance After even, in second beds of feeding.
Using benzene, as oxidant hydrogen peroxide (in the form of 40 weight % hydrogen peroxide provide) and Reaction raw materials are mixed to form as the acetone of solvent, ammoniacal liquor is added into reaction raw materials, and (concentration is 30 weights Measure %), the pH value of reaction raw materials is adjusted to 7.0, reaction raw materials are sent into fixed bed reaction from bottom In device and flow through beds, with HTS haptoreaction.Wherein, benzene and hydrogen peroxide Mol ratio is 1：0.5, the mol ratio of benzene and acetone is 1：6.Temperature in reactor is 35 DEG C, instead Should during by the Stress control in fixed bed reactors be 1.5MPa, the weight (hourly) space velocity (WHSV) of benzene is 4.5h-1。
The reactant mixture exported from reactor is flashed, gas stream and liquids is separated into Stream.Gas stream condenses benzene by cooling, to reclaim benzene；Liquid stream is distilled, and is collected respectively Water, acetone and phenol, phenol is exported.The benzene and acetone of recovery is well mixed rear directly (being 25 DEG C) Sent into as carrying object between first beds and the second beds, the feeding amount of carrying object So that v2/v1=5, v1For the superficial velocity of reaction stream in first beds, v2For second The superficial velocity of reaction stream in beds.
The reaction exported from second fixed bed reactors is monitored in course of reaction using gas-chromatography to mix The composition of compound, and calculate benzene conversion ratio, oxidant effective rate of utilization and phenol selectivity, reaction result Listed in table 2.
Embodiment 12
Using with the identical method of embodiment 11 by benzene oxidatoin, unlike, in first catalyst bed The loadings of layer and second beds under the same conditions, are urged with embodiment 11 at second The titanium-silicon molecular sieve TS-1 that filling is prepared using the method for embodiment 1 in agent bed.Reaction result is in table Listed in 2.
Embodiment 13
Using with the identical method of embodiment 11 by benzene oxidatoin, unlike, in first catalyst bed Under conditions of the loadings of layer and second beds keep constant, hollow TS-1 titaniums silicon molecule Sieve is modified processing before as catalyst using following methods；And in second beds The titanium-silicon molecular sieve TS-1 of modification prepared by middle filling embodiment 8.
By hollow TS-1 HTSs with containing HNO3(HNO3Mass concentration 10%) and mistake for The aqueous solution mixing of hydrogen oxide (mass concentration of hydrogen peroxide is 5%), by obtained mixture in close The stirring reaction 4h under 120 DEG C of pressure itselfs is closed in container, the temperature of obtained reactant mixture is down to room Filtered after temperature, obtained solid matter is dried to constant weight at 120 DEG C, obtain modified titanium silicon point Son sieve.Wherein, hollow HTS is with SiO2Count, the mol ratio of HTS and hydrogen peroxide is 1：0.4.Compared with raw material HTS, in the UV-Vis spectrum of the HTS of obtained modification The peak area of absworption peak between 230-310nm reduces 4.6%, by the hole of static determination of nitrogen adsorption Hold and reduce 3.8%.Reaction result is listed in table 2.
Table 2
Embodiment 14
The titanium-silicon molecular sieve TS-1 used in the present embodiment is prepared using following methods.
First butyl titanate is dissolved in the alkali source template TPAOH aqueous solution, silicon is then added Glue (is purchased from Qingdao silica gel factory), obtains dispersion liquid, in the dispersion liquid, silicon source：Titanium source：Alkali source template Agent：The mol ratio of water is 100：2：10：600, silicon source is with SiO2Meter, titanium source is with TiO2Meter, alkali Source template is in terms of N.10h are stood at 40 DEG C after above-mentioned dispersion liquid is sealed in beaker using sealed membrane, 0.5h is stirred at 25 DEG C followed by magnetic agitation, is allowed to disperse again.By point after disperseing again Dispersion liquid is transferred in sealing reactor, is undergone first stage crystallization 8h at 130 DEG C, is then dropped mixture Temperature to 50 DEG C of experience second stage are stopped after 5h, are continued in sealing reactor at a temperature of 170 DEG C Phase III crystallization 16h is undergone (wherein, by the heating rate of room temperature to first stage crystallization temperature It it is 10 DEG C by the rate of temperature fall of first stage crystallization temperature to second stage treatment temperature for 1 DEG C/min / min, is 20 DEG C/min by the heating rate of second stage treatment temperature to phase III crystallization temperature), Without filtering and washing step after gained crystallization product is taken out, directly 3h, Ran Hou are dried in 120 DEG C 2h is calcined at 580 DEG C, molecular sieve is obtained.The XRD crystalline phases figure of gained sample is prepared with embodiment 1 Titanium-silicon molecular sieve TS-1 is consistent, and illustrate to obtain is the titanium-silicon molecular sieve TS-1 with MFI structure；Fu In vertical leaf transformation infrared spectrogram, in 960cm-1Nearby there is absworption peak, show that titanium has been enter into molecular sieve In skeleton, the HTS, surface silicon titanium ratio/body phase silicon titanium ratio is 2.25, and titanium oxide content is 2.6 Weight %.By the former powder of obtained titanium-silicon molecular sieve TS-1 and Ludox, pore-foaming agent (alkyl phenol polyoxy second Alkene ether) and starch mixing, extrusion is carried out using banded extruder, then grain is prepared through pelletizing, drying and roasting For 500 microns of titanium-silicon molecular sieve TS-1 catalyst, (wherein, the quality percentage of HTS contains in footpath Measure as 85%).
By Catalyst packing in draw ratio in 50 isometrical fixed bed reactors, to form beds, Wherein, the quantity of beds is 2 layers, and 2 layers of beds are arranged in parallel, spacing 50cm；The One beds loads hollow HTS (identical with embodiment 11), second catalyst bed Layer filling titanium-silicon molecular sieve TS-1 manufactured in the present embodiment, first beds and second catalyst The weight ratio of the loadings of bed is 8：1, respectively 800g and 100g.Two layers beds it Between carrying object entrance and liquid distributor be set, liquid distributor is used to be sent into by carrying object entrance After carrying object is well mixed with the effluent of first beds, second beds is sent into In.
Using benzene, that the TBHP as oxidant and the acetonitrile as solvent are mixed to form reaction is former Material, ammoniacal liquor (concentration is 40 weight %) is added into reaction raw materials, the pH value of reaction raw materials is adjusted For 6.9, by reaction raw materials from bottom send into fixed bed reactors in and flow through beds, with titanium Si molecular sieves haptoreaction.Wherein, the mol ratio of benzene and TBHP is 1：1, benzene and acetonitrile Mol ratio be 1：8.Temperature in reactor is 50 DEG C, by fixed bed reactors in course of reaction Stress control be 2.0MPa, the weight (hourly) space velocity (WHSV) of benzene is 20h-1。
The reactant mixture exported from reactor is flashed, gas stream and liquids is separated into Stream.Wherein, gas stream condenses benzene by cooling, to reclaim benzene；Liquid stream is distilled, point Not Shou Ji acetonitrile and phenol, phenol is exported.50 DEG C are heated to after the benzene and acetonitrile of recovery are well mixed Sent into as carrying object between first beds and the second beds, the feeding amount of carrying object So that v2/v1=3.5, v1For the superficial velocity of reaction stream in first beds, v2For second The superficial velocity of reaction stream in individual beds.
The reaction exported from second fixed bed reactors is monitored in course of reaction using gas-chromatography to mix The composition of compound, and calculate benzene conversion ratio, oxidant effective rate of utilization and phenol selectivity, reaction result Listed in table 3.
Embodiment 15
Using with the identical method of embodiment 14 by benzene oxidatoin, unlike, first beds The titanium silicon drawn off from propylene ring oxidation reaction device through regeneration is loaded with second beds (titanium-silicon molecular sieve TS-1 is used to be prepared molecular sieve TS-1 with the identical method of embodiment 14, is drawn off HTS is calcined 3h in air atmosphere at a temperature of 580 DEG C and regenerated, and the activity after regeneration is 40%, 95%) activity when fresh is.Reaction result is listed in table 3.
Embodiment 16
Using with the identical method of embodiment 15 by benzene oxidatoin, unlike, the titanium silicon molecule through regeneration TS-1 is sieved before as catalyst, processing is modified using following methods.
With containing HNO3(HNO3Mass concentration 15%) and the hydrogen peroxide (matter of hydrogen peroxide for It is aqueous solution mixing 8%) to measure concentration, and obtained mixture is stirred in closed container at 150 DEG C 3h is reacted, the temperature of obtained reactant mixture, which is down to after room temperature, to be filtered, by obtained solid matter Dried at 120 DEG C to constant weight, obtain modified HTS.Wherein, titanium-silicon molecular sieve TS-1 with SiO2The mol ratio of meter, HTS and hydrogen peroxide is 1：2.Compared with raw material HTS, The peak of absworption peak in the UV-Vis spectrum of the HTS of obtained modification between 230-310nm Area reduces 5.3%, and 4.8% is reduced by the pore volume of static determination of nitrogen adsorption.Reaction result is in table 3 List.
Embodiment 17
The titanium-silicon molecular sieve TS-1 used in the present embodiment is prepared using following methods.
First butyl titanate is dissolved in the alkali source template TPAOH aqueous solution, silicon is then added Glue (is purchased from Qingdao silica gel factory), obtains dispersion liquid, in the dispersion liquid, silicon source：Titanium source：Alkali source template Agent：The mol ratio of water is 100：5：18：1000, silicon source is with SiO2Meter, titanium source is with TiO2Meter, alkali Source template is in terms of N.After above-mentioned dispersion liquid is sealed in beaker using sealed membrane 8h are stood at 45 DEG C； Dispersion liquid through standing is transferred in sealing reactor, first stage crystallization 6h is undergone at 140 DEG C, connects By mixture be cooled to 40 DEG C experience second stage stop 1h after, continue sealing reactor in Phase III crystallization 12h is undergone at a temperature of 160 DEG C (wherein, by room temperature to first stage crystallization temperature The heating rate of degree is 5 DEG C/min, by the cooling of first stage crystallization temperature to second stage treatment temperature Speed is 5 DEG C/min, is 5 DEG C by the heating rate of second stage treatment temperature to phase III crystallization temperature / min), without filtering and washing step after gained crystallization product is taken out, 2h directly is dried in 110 DEG C, Then 3h is calcined at 550 DEG C, molecular sieve is obtained.The XRD crystalline phases figure of gained sample and embodiment 1 The titanium-silicon molecular sieve TS-1 of preparation is consistent, and illustrate to obtain is the HTS with MFI structure TS-1；In FFIR figure, in 960cm-1Nearby there is absworption peak, show that titanium has entered Enter framework of molecular sieve, in the HTS, surface silicon titanium ratio/body phase silicon titanium ratio is 2.71, and titanium oxide contains Measure as 4.3 weight %.By the former powder of obtained titanium-silicon molecular sieve TS-1 and Ludox, pore-foaming agent (alkyl phenol APEO) and starch mixing, extrusion is carried out using banded extruder, then make through pelletizing, drying and roasting It is standby go out particle diameter be 500 microns of titanium-silicon molecular sieve TS-1 catalyst (wherein, the quality of HTS 85%) percentage composition is.
By Catalyst packing in draw ratio in 5 isometrical fixed bed reactors, to form beds, Wherein, the quantity of beds is 2 layers, and 2 layers of beds are arranged in parallel, spacing 5cm；The One beds loads hollow HTS (identical with embodiment 11), second catalyst bed Titanium-silicon molecular sieve TS-1 prepared by layer filling embodiment 17, first beds and second catalysis The weight ratio of the loadings of agent bed is 4：1, respectively 800g and 200g.In two layers of beds Between carrying object entrance and liquid distributor are set, liquid distributor is used to be sent into by carrying object entrance Carrying object be well mixed with the effluent of first beds after, send into second beds In.
Using benzene, that the cumyl hydroperoxide as oxidant and the acetonitrile as solvent are mixed to form reaction is former Material, ammoniacal liquor (concentration is 25 weight %) is added into reaction raw materials, the pH value of reaction raw materials is adjusted For 6.8, by reaction raw materials from bottom send into fixed bed reactors in and flow through beds, with titanium Si molecular sieves haptoreaction.Wherein, the mol ratio of benzene and cumyl hydroperoxide is 1：1, benzene and acetonitrile Mol ratio be 1：6.Temperature in reactor is 60 DEG C, by fixed bed reactors in course of reaction Stress control be 1.8MPa, the weight (hourly) space velocity (WHSV) of benzene is 1.5h-1。
The reactant mixture exported from reactor is flashed, gas stream and liquids is separated into Stream.Wherein, gas stream condenses benzene by cooling, to reclaim benzene；Liquid stream is distilled, point Not Shou Ji acetonitrile and phenol, phenol is exported.The benzene and acetonitrile of recovery are well mixed and 60 DEG C are heated to Sent into afterwards as carrying object between first beds and the second beds, the feeding of carrying object Amount causes v2/v1=4, v1For the superficial velocity of reaction stream in first beds, v2For second The superficial velocity of reaction stream in individual beds.
The reaction exported from second fixed bed reactors is monitored in course of reaction using gas-chromatography to mix The composition of compound, and calculate benzene conversion ratio, oxidant effective rate of utilization and phenol selectivity, reaction result Listed in table 3.
Table 3
Embodiment 18
Using titanium-silicon molecular sieve TS-1 catalyst same as Example 1, by Catalyst packing in draw ratio In 25 isometrical fixed bed reactors, to form beds, wherein, the quantity of beds For 4 layers, 4 layers of beds equidistant parallel arrangement, spacing 10cm；Loaded in four beds Catalyst identical in quality, respectively 200g.Respectively first, second, and third, the 4th layer of catalysis Carrying object entrance and liquid distributor are set between agent bed, and liquid distributor is used to by carrying object to be entered After the carrying object of mouth feeding is well mixed with the effluent of first or the 3rd beds, feeding second Or in the 4th beds.
Using benzene, as oxidant hydrogen peroxide (in the form of 30 weight % hydrogen peroxide provide) and Reaction raw materials are mixed to form as the methanol of solvent, during reaction raw materials are sent into fixed bed reactors from bottom And flow through beds, with HTS haptoreaction.Wherein, mole of benzene and hydrogen peroxide Than for 1：1, the mol ratio of benzene and methanol is 1：16.Temperature in reactor is 30 DEG C, course of reaction The middle Stress control by fixed bed reactors is 0.5MPa, and the weight (hourly) space velocity (WHSV) of benzene is 5h-1。
The reactant mixture exported from reactor is flashed, gas stream and liquids is separated into Stream.Wherein, gas stream condenses benzene by cooling, to reclaim benzene；Liquid stream is distilled, point Not Shou Ji methanol, water and phenol, phenol is exported.It is heated to after the benzene and methanol of recovery are well mixed 30 DEG C are sent into first beds and the second beds, the 3rd catalyst bed as carrying object Between layer and the 4th beds, the feeding amount of carrying object causes v2/v1=2, v4/v3=2, v1 For the superficial velocity of reaction stream in first beds, v2To be reacted in second beds The superficial velocity of logistics, v3For the superficial velocity of reaction stream in the 3rd beds, v4For the 4th The superficial velocity of reaction stream in individual beds.
The reaction exported from the 4th fixed bed reactors is monitored in course of reaction using gas-chromatography to mix The composition of compound, and calculate benzene conversion ratio, oxidant effective rate of utilization and phenol selectivity, reaction result Listed in table 4.
Embodiment 19
Using with the identical method of embodiment 18 by benzene oxidatoin, unlike, in four beds Loadings keep constant under conditions of, first beds load hollow HTS (with Embodiment 11 is identical), titanium silicon molecule prepared by second to the 4th beds filling embodiment 14 Sieve TS-1.Reaction result is listed in table 4.
Table 4
Embodiment 20
Using with the identical method of embodiment 18 by toluene oxidation.Reaction result is listed in table 5.
Table 5
The preferred embodiment of the present invention is described in detail above in association with accompanying drawing, still, the present invention is not limited Detail in above-mentioned embodiment, can be to the present invention in the range of the technology design of the present invention Technical scheme carry out a variety of simple variants, these simple variants belong to protection scope of the present invention.
It is further to note that each particular technique described in above-mentioned embodiment is special Levy, in the case of reconcilable, can be combined by any suitable means.In order to avoid need not The repetition wanted, the present invention no longer separately illustrates to various possible combinations.
In addition, various embodiments of the present invention can be combined randomly, as long as its Without prejudice to the thought of the present invention, it should equally be considered as content disclosed in this invention.

Claims (23)

1. a kind of aromatic oxidation process, this method is included under oxidation reaction condition, make containing at least one The reaction feed for planting aromatic hydrocarbons, oxidant and optional at least one solvent flows successively through the 1st beds To the n-th last beds, n is more than 2 integer, is loaded in each beds There is at least one HTS, it is characterised in that pass through the 1st beds in reaction feed During n catalyst bed, to the 1st beds at least one pair of phase between the n-th beds Carrying object is introduced between adjacent beds so that on the basis of the flow direction of reaction feed, this at least one To in adjacent beds, the superficial velocity of reaction stream is higher than in the beds in downstream The superficial velocity of reaction stream in the beds of upstream.
2. according to the method described in claim 1, wherein, in the pair of adjacent beds In, the superficial velocity of reaction stream is expressed as v in the beds in downstreamm, it is described to be located at upstream Beds in the superficial velocity of reaction stream be expressed as vm-1, the introduction volume of the carrying object causes vm/vm-1=1.5-15, it is preferable that vm/vm-1=2-10, more preferably causes vm/vm-1=2-5.
3. according to the method described in claim 1, wherein, the carrying object be selected from non-active gas, At least one of the effluent of beds and the solvent；The effluent of the beds is From the outflow of at least one beds outflow of the 1st beds into the n-th beds Thing；
Preferably, the carrying object is the effluent of n-th beds；
It is highly preferred that the carrying object is to isolate target from the effluent of n-th beds Remaining logistics after arene oxidizing thing.
4. the method according to any one in claim 1-3, wherein, the HTS The HTS being at least partially modified, the HTS of the modification is the titanium of experience modification Si molecular sieves, the modification include using as the HTS of raw material with containing nitric acid and peroxidating The modification liquid contact of thing.
5. method according to claim 4, wherein, in the modification, the conduct The mol ratio of the HTS of raw material and the peroxide is 1：(0.01-5), preferably 1： (0.05-3), more preferably 1：The mol ratio of (0.1-2), the peroxide and the nitric acid is 1： (0.01-50), preferably 1：(0.1-20), more preferably 1：(0.2-10), more preferably 1： (0.5-5), particularly preferably 1：(0.6-3.5), the HTS is in terms of silica.
6. method according to claim 4, wherein, in the modification liquid, the peroxide 0.1-50 weight %, preferably 0.5-25 weight %, more preferably 5-15 are respectively with the concentration of the nitric acid Weight %.
7. method according to claim 4, wherein, in the modification, the conduct The HTS of raw material and the modification liquid 10-350 DEG C, preferably 20-300 DEG C, more preferably exist 50-250 DEG C, further preferably contacted at a temperature of 60-200 DEG C, the contact is in pressure Carried out in 0-5MPa container, the pressure is gauge pressure, and the duration of the contact is 1-10 hours, Preferably 3-5 hours.
8. method according to claim 4, wherein, the peroxide be selected from hydrogen peroxide, TBHP, cumyl hydroperoxide, ethylbenzene hydroperoxide, cyclohexyl hydroperoxide, peroxide At least one of acetic acid and Perpropionic Acid.
9. method according to claim 4, wherein, in the modification, the conduct The exposure level of the HTS of raw material and the modification liquid causes, using the HTS as raw material On the basis of, in ultraviolet-visible spectrum, the HTS of the modification is between 230-310nm The peak area reduction by more than 2% of absworption peak, preferably reduces 2-30%, more preferably reduces 2.5-15%, enter one The preferred reduction 3-10% of step, still more preferably reduces 3-6%；The hole of the HTS of the modification Hold and reduce more than 1%, preferably reduce 1-20%, more preferably reduce 1.5-10%, further preferably reduce 2-5%, the pore volume is using static determination of nitrogen adsorption.
10. according to the method described in claim 1, wherein, the HTS is at least partly originated In the agent that draws off of reaction unit after regeneration, the reaction unit after regeneration draw off agent be selected from Ammoximation reaction device after regeneration draws off unloading for agent and/or epoxidation reaction device after regeneration Go out agent.
11. according to the method described in claim 1, wherein, the HTS at least partially titanium Silicalite TS-1, the surface silicon titanium ratio of the titanium-silicon molecular sieve TS-1 is not less than body phase silicon titanium ratio, institute Mol ratio of the silicon titanium than referring to silica and titanium oxide is stated, the surface silicon titanium ratio uses x-ray photoelectron Spectroscopy is determined, and the body phase silicon titanium ratio uses x-ray fluorescence spectrometry；
Preferably, the surface silicon titanium than with the body phase silicon titanium than ratio be more than 1.2；
It is highly preferred that the surface silicon titanium than with the body phase silicon titanium than ratio be 1.2-5；
It is further preferred that the surface silicon titanium than with the body phase silicon titanium than ratio be 1.5-4.5.
12. method according to claim 11, wherein, the titanium-silicon molecular sieve TS-1 is using bag It is prepared by the method for including following steps：
(A) inorganic silicon source is dispersed in the aqueous solution containing titanium source and alkali source template, and alternatively Water is supplemented, is obtained in dispersion liquid, the dispersion liquid, silicon source：Titanium source：Alkali source template：Mole of water Than for 100：(0.5-8)：(5-30)：(100-2000), the inorganic silicon source is with SiO2Meter, the titanium Source is with TiO2Meter, the alkali source template is in terms of OH- or N；
(B) dispersion liquid for obtaining step (A) stands 6-24 hours at 15-60 DEG C；
(C) dispersion liquid that the dispersion liquid or step (B) obtained step (A) is obtained is anti-in sealing Stage (1) of sequentially being undergone in kettle, stage (2) and stage (3) is answered to carry out crystallization, the stage (1) exists 80-150 DEG C, preferably 110-140 DEG C, more preferably 120-140 DEG C, further preferably at 130-140 DEG C Crystallization 6-72 hours, preferably 6-8 hours, the stage (2) was cooled to not higher than 70 DEG C and residence time extremely Less be 0.5 hour, preferably 1-5 hours, the stage (3) be warming up to 120-200 DEG C, preferably 140-180 DEG C, More preferably at 160-170 DEG C, then crystallization 6-96 hours, preferably 12-20 hours.
13. method according to claim 12, wherein, the stage (1) and the stage (3) Meet one or both of following condition：
Condition 1：The crystallization temperature of the stage (1) is less than the crystallization temperature in the stage (3), excellent Selection of land, the crystallization temperature of the stage (1) is lower 10-50 DEG C than the crystallization temperature in the stage (3), It is more preferably low 20-40 DEG C；
Condition 2：The crystallization time of the stage (1) is less than the crystallization time in the stage (3), excellent Selection of land, the crystallization time of the stage (1) is shorter 5-24 hours than the crystallization time in the stage (3), It is more preferably short 6-12 hours.
14. method according to claim 12, wherein, the stage (2) is cooled to not higher than 50 DEG C, and the residence time be at least 1 hour.
15. method according to claim 12, wherein, the titanium source is inorganic titanium salt and/or had Organic titanate, the inorganic titanium salt is selected from TiCl4、Ti(SO4)2And TiOCl2At least one of, institute Organic titanate is stated for general formula R7 4TiO4The compound of expression, R7For the alkyl with 2-4 carbon atom； The alkali source template is selected from least one of quaternary ammonium base, aliphatic amine and aliphatic hydramine, preferably For quaternary ammonium base, more preferably TPAOH；The inorganic silicon source is silica gel and/or Ludox.
16. according to the method described in claim 1, wherein, the titanium of the 1st beds filling Si molecular sieves are hollow titanium-silicon molecular sieve TS-1, the titanium silicon of the 2nd to the n-th beds filling Molecular sieve is non-hollow titanium-silicon molecular sieve TS-1.
17. according to the method described in claim 1, wherein, the 1st beds are to last Filled in n-th beds in any pair of adjacent beds in the beds in downstream The quality representation for the catalyst filled out is Wm, the matter of the catalyst loaded in the beds of upstream Amount is expressed as Wm-1, Wm-1/WmFor 0.1-20, preferably 2-8, m is any whole in [2, n] interval Number.
18. according to the method described in claim 1, wherein, mole of the aromatic hydrocarbons and the oxidant Than for (0.1-20)：1, be preferably (0.2-10)：1, more preferably (1-5)：1.
19. according to the method described in claim 1, wherein, the oxidant be selected from hydrogen peroxide, TBHP, ethylbenzene hydroperoxide, cumyl hydroperoxide, cyclohexyl hydroperoxide, peroxide At least one of acetic acid and Perpropionic Acid.
20. according to the method described in claim 1, wherein, the solvent be selected from water, C1-C10 Alcohol, C3-C10 ketone, at least one of C2-C10 nitrile and C1-C6 carboxylic acid；Preferably, The solvent is at least one of nitrile of the alcohol selected from C1-C6, C3-C8 ketone and C2-C5；It is more excellent Selection of land, the solvent is selected from methanol, ethanol, acetonitrile, normal propyl alcohol, isopropanol, the tert-butyl alcohol, isobutyl At least one of alcohol and acetone；It is further preferred that the solvent is selected from methanol, acetonitrile, acetone At least one of with the tert-butyl alcohol.
21. according to the method described in claim 1, wherein, this method also includes to the reaction feed The middle at least one alkaline matter of feeding, the feeding amount of the alkaline matter causes the pH of the reaction feed Value is in the range of 6-9.
22. according to the method described in claim 1, wherein, the aromatic hydrocarbons be selected from benzene, toluene, two At least one of toluene, ethylbenzene, isopropylbenzene.
23. according to the method described in claim 1, wherein, the oxidation reaction condition includes：Temperature For 0-120 DEG C, preferably 20-80 DEG C, more preferably 30-60 DEG C；Pressure is 0-3MP, is preferably 0.1-2.5MPa, the pressure is gauge pressure.
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CN104944441A (en) * 2014-03-31 2015-09-30 中国石油化工股份有限公司 Method for synthesizing titanium-silicon molecular sieve
CN104291352A (en) * 2014-09-30 2015-01-21 浙江大学 Method for preparing and modifying titanium silicalite molecular sieve catalyst and application of titanium silicalite molecular sieve catalyst in ketone oximation

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CN110128250A (en) * 2018-02-09 2019-08-16 中国石油化工股份有限公司 The method for preparing cyclohexanone
CN110128250B (en) * 2018-02-09 2021-10-08 中国石油化工股份有限公司 Process for preparing cyclohexanone
CN111116321A (en) * 2020-01-21 2020-05-08 山东理工大学 Green synthesis method for preparing phenol by benzene hydroxylation
CN111116321B (en) * 2020-01-21 2023-01-03 山东理工大学 Green synthesis method for preparing phenol by benzene hydroxylation

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