CN108329191B - Method for processing cyclohexane oxidation liquid - Google Patents
Method for processing cyclohexane oxidation liquid Download PDFInfo
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- CN108329191B CN108329191B CN201810080571.9A CN201810080571A CN108329191B CN 108329191 B CN108329191 B CN 108329191B CN 201810080571 A CN201810080571 A CN 201810080571A CN 108329191 B CN108329191 B CN 108329191B
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- C07—ORGANIC CHEMISTRY
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- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/51—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by pyrolysis, rearrangement or decomposition
- C07C45/53—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by pyrolysis, rearrangement or decomposition of hydroperoxides
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- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
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Abstract
The invention relates to the field of fine chemical engineering, and particularly provides a method for processing cyclohexane oxidation liquid, which comprises the following steps: the method comprises the following steps of (1) contacting cyclohexane oxidation liquid with a catalyst, wherein the catalyst contains a silicon-containing molecular sieve, the cyclohexane oxidation liquid contains cyclohexyl hydroperoxide, and the preparation method of the silicon-containing molecular sieve comprises the following steps: (1) hydrolyzing a silicon source, a VIII group metal source and a structure directing agent to obtain a hydrolyzed material; (2) crystallizing the hydrolyzed material; wherein, the step (1) is carried out in the presence of an organic phosphorus compound and/or before the step (2), the hydrolyzed material is mixed with the organic phosphorus compound and then the crystallization is carried out. The silicon-containing molecular sieve is used for processing cyclohexane oxidation liquid, no additional alkaline reagent is needed to be added, the reaction effects of high alcohol-ketone ratio and high alcohol-ketone selectivity can be obtained at a lower temperature, and the silicon-containing molecular sieve has high industrial application value.
Description
Technical Field
The invention relates to a method for processing cyclohexane oxidation liquid.
Background
Cyclohexanone is an important basic chemical raw material, and has been used for producing important chemical products such as caprolactam, adipic acid, epsilon-caprolactone and the like. According to statistics, the capacity of cyclohexanone in China reaches 365 ten thousand tons by 2015 years. The cyclohexanone is mainly produced by cyclohexane oxidation and cyclohexene hydration processes in China, and the ratio of the capacity of the cyclohexane oxidation is up to 63%.
The prior cyclohexane oxidation process mainly comprises three working procedures of cyclohexane oxidation, cyclohexyl hydrogen peroxide decomposition and cyclohexanol dehydrogenation. Although the cyclohexanol dehydrogenation process is relatively mature and stable, the side reaction of the cyclohexane oxidation process is more, the cyclohexane conversion rate is not higher than 4%, and the decomposition of the cyclohexyl hydroperoxide is restricted by the problems of low alcohol ketone yield (< 88%), large three-waste discharge amount, difficult treatment and the like.
Cyclohexyl hydroperoxide decomposition is an important step of the oxidation process for preparing cyclohexanone, and the existing process is generally that under alkaline conditions (38-42% NaOH solution), a trace amount of soluble cobalt salt catalyzes the decomposition of cyclohexyl hydroperoxide into cyclohexanol and cyclohexanone. Under the process condition, cyclohexanol and cyclohexanone can be further condensed, so that the yield of alcohol ketone is reduced; the cobalt salt can not be recovered and can react with a small amount of organic acid in the cyclohexyl hydroperoxide solution to form precipitate, which can cause the problems of pipeline blockage and the like; 1-1.2 tons of inorganic alkali waste liquid can be produced when 1 ton of cyclohexanone is produced, and the waste liquid contains a large amount of organic matters, so that the organic matters are difficult to recycle, the waste water treatment is difficult, and the cost is high.
In order to solve the problems of inorganic alkali/cobalt salt systems, heterogeneous catalytic materials have been developed. DuPont company has developed supported catalytic materials with activated alumina, silica, titania or activated carbon as the support and iron oxide, cobalt oxide, nickel oxide, manganese oxide, niobium oxide or noble metals as the active site (US2851496, US4503257, WO9809931, US 4720592); the basf company uses molecular sieve, iron oxide, cobalt oxide and nickel oxide as catalyst carrier and active component, and studies the decomposition performance of cyclohexyl hydroperoxide of the supported catalyst (US 4491637); the Tesmann company has developed supported catalysts with chromium oxide, copper-chromium complex oxides, phthalocyanines or purine metal compounds as active components (US 3941845, US 3987101, US 4042630, CN 89108142.9, CN 91103225). Furthermore, heteroatom molecular sieves, including Cr-AFI (Sheldon R A, Chen J D, Dakka J, et al Studies in surface Science and Catalysis,1994,82: 515-.
Although the acting force between the metal oxide and the carrier is weak, the stability of the supported catalytic material needs to be improved; in the supported catalyst, the content of the metal oxide is high (> 1% mass fraction), which makes it difficult to ensure that the active component can be uniformly distributed; the sizes of the pore passages of the AFI and MFI structures are not more than 0.55nm, the molecular size of the cyclohexyl hydroperoxide is about 0.74nm, the Cr active centers in the two molecular sieves are difficult to react with CHHP, and the effective utilization rate of the active centers of the heteroatom molecular sieves is low; although the mesoporous TUD has a larger pore channel structure, the pore wall of the mesoporous TUD is amorphous, and the hydrothermal stability of the mesoporous TUD is not ideal.
By combining the above analysis, in order to solve the problems of the existing homogeneously catalyzed cyclohexyl hydroperoxide decomposition process, the development of a heterogeneous catalytic material is a key point, and further intensive research is needed to prepare a cyclohexyl hydroperoxide decomposition catalyst with highly dispersed active components, good accessibility of active centers and good hydrothermal stability.
Disclosure of Invention
The invention aims to provide a method for processing cyclohexane oxidation liquid, which has high selectivity of alcohol and ketone and high alcohol and ketone ratio.
In order to achieve the foregoing object, the present invention provides a method for processing an oxidized cyclohexane liquid, comprising: contacting cyclohexane oxidation liquid with a catalyst, wherein the cyclohexane oxidation liquid contains cyclohexyl hydrogen peroxide, the catalyst contains a silicon-containing molecular sieve, and the preparation method of the silicon-containing molecular sieve comprises the following steps: (1) hydrolyzing a silicon source, a VIII group metal source and a structure directing agent to obtain a hydrolyzed material; (2) crystallizing the hydrolyzed material; wherein, the step (1) is carried out in the presence of an organic phosphorus compound and/or before the step (2), the hydrolyzed material is mixed with the organic phosphorus compound and then the crystallization is carried out.
The catalyst of the invention is used for processing cyclohexane oxidation liquid, no additional alkaline reagent is needed to be added, the reaction effects of high alcohol-ketone ratio and high alcohol-ketone selectivity can be obtained at a lower temperature, and the catalyst has high industrial application value.
As shown in the following formula:
cyclohexyl hydroperoxide is the main product of selective hydrogenation of cyclohexane, and its catalytic decomposition products mainly comprise cyclohexanol and cyclohexanone.
When cyclohexanone is selectively generated, although the energy consumption is relatively reduced, one molecular hydrogen resource is converted into water, the utilization rate of the hydrogen resource is relatively low, and the load of a subsequent water treatment device is increased.
When cyclohexanol is selectively generated, cyclohexanol is dehydrogenated to generate cyclohexanone, so that generated hydrogen can be recycled for a benzene hydrogenation process, and the effective utilization rate of hydrogen resources is improved. Namely, the method can greatly improve the utilization rate of hydrogen atoms and provides a feasible choice for industrial implementation.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Detailed Description
The following describes in detail specific embodiments of the present invention. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.
The invention provides a method for processing cyclohexane oxidation liquid, which comprises the following steps: contacting cyclohexane oxidation liquid with a catalyst, wherein the cyclohexane oxidation liquid contains cyclohexyl hydrogen peroxide, the catalyst contains a silicon-containing molecular sieve, and the preparation method of the silicon-containing molecular sieve comprises the following steps: (1) hydrolyzing a silicon source, a VIII group metal source and a structure directing agent to obtain a hydrolyzed material; (2) crystallizing the hydrolyzed material; wherein, the step (1) is carried out in the presence of an organic phosphorus compound and/or before the step (2), the hydrolyzed material is mixed with the organic phosphorus compound and then the crystallization is carried out.
In the present invention, the organophosphorus compound refers to a phosphorus-containing organic compound.
The catalyst of the invention is used for processing cyclohexane oxidation liquid, no additional alkaline reagent is needed to be added, the reaction effects of high alcohol-ketone ratio and high alcohol-ketone selectivity can be obtained at a lower temperature, and the catalyst has high industrial application value.
According to the method of the present invention, the cyclohexane oxidation liquid generally contains cyclohexanol, cyclohexanone and cyclohexane in addition to cyclohexyl hydroperoxide, and there is no special requirement for the composition of each substance, and any cyclohexane oxidation liquid containing the above substances can be used in the present invention.
According to a preferred embodiment of the present invention, the cyclohexane oxidation liquid contains 3.0 to 3.6 wt% of cyclohexyl hydroperoxide, 0.6 to 1.0 wt% of cyclohexanol, 0.4 to 0.7 wt% of cyclohexanone, 0.15 to 0.3 wt% of organic acid, 0.2 to 0.4 wt% of organic ester, and 94.00 to 95.65 wt% of cyclohexane.
According to the above technical solution, the object of the present invention can be achieved, and for the present invention, the molar ratio of the organic phosphorus compound to the silicon source is preferably P: SiO 22(0.001-0.5): 1, more preferably P: SiO 22(0.1-0.3): 1. therefore, the performance of the silicon-containing molecular sieve can be improved, for example, the catalytic decomposition performance of the silicon-containing molecular sieve used as a catalyst for processing cyclohexane oxidation liquid can be improved, the alcohol ketone ratio is greatly improved, and the alcohol ketone selectivity is high.
According to a preferred embodiment of the present invention, the preparation method comprises:
(1) hydrolyzing a silicon source, a VIII group metal source, a first part of organic phosphorus compound and a structure directing agent to obtain a hydrolyzed material;
(2) and mixing the hydrolyzed material with a second part of organic phosphorus compound, and then carrying out crystallization. According to the steps, the performance of the silicon-containing molecular sieve can be further improved, for example, the catalytic decomposition performance of the silicon-containing molecular sieve serving as a catalyst for processing cyclohexane oxidation liquid can be improved, the alcohol-ketone ratio is greatly improved, and the alcohol-ketone selectivity is high.
According to the process of the present invention, it is preferred that the first portion of the organic phosphorus compounds is used in an amount of 10 to 90% by weight and the second portion of the organic phosphorus compounds is used in an amount of 10 to 90% by weight, based on 100% by weight of the total amount of the organic phosphorus compounds; more preferably, the first portion of the organophosphorus compound is used in an amount of 30 to 40 wt%, and the second portion of the organophosphorus compound is used in an amount of 60 to 70 wt%.
According to the process of the present invention, it is preferred that the conditions under which the said hydrolysable material is mixed with the organophosphorus compound comprise: the temperature is 60-100 deg.C, preferably 70-90 deg.C. Therefore, the performance of the silicon-containing molecular sieve can be further improved, for example, the catalytic decomposition performance of the silicon-containing molecular sieve used as a catalyst for processing cyclohexane oxidation liquid can be improved, the alcohol-ketone ratio is greatly improved, and the alcohol-ketone selectivity is high.
More preferably, the conditions under which the hydrolysed material is mixed with the organophosphorus compound according to the process of the present invention comprise: the time is 1-10h, preferably 2-4 h.
Group VIII metals may be used in the present invention according to the process of the present invention, and for the purposes of the present invention preferably the group VIII metal is one or more of cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium and platinum, more preferably cobalt.
According to the process of the invention, the hydrolysis of the silicon source, the group VIII metal source and the structure directing agent is preferably carried out in the presence of a silylating agent and/or the hydrolysis mass is mixed with an organophosphorus compound in the presence of a silylating agent; more preferably, the molar ratio of the silicon source to the silylation agent is SiO2: silylation reagent ═ 1: (0.001-0.1), preferably SiO2: silylation reagent ═ 1: (0.01-0.06).
According to a preferred embodiment of the invention, the method comprises: (1) hydrolyzing a silicon source, a VIII group metal source, a first part of organic phosphorus compound and a structure directing agent to obtain a hydrolyzed material;
(2) and mixing the hydrolyzed material, a second part of organic phosphorus compound and a silanization reagent for crystallization.
Preferably, the first portion of the organic phosphorus compound is present in an amount of 10 to 90 wt.%, the second portion of the organic phosphorus compound is present in an amount of 10 to 90 wt.%, and the molar ratio of the silicon source to the silylating agent is SiO, based on 100 wt.% of the total amount of the organic phosphorus compounds present2: silylation reagent ═ 1: (0.001-0.1); preferably, the first portion of the organophosphorus compound is used in an amount of 30 to 40 wt%, the second portion of the organophosphorus compound is used in an amount of 60 to 70 wt%, and the molar ratio of the silicon source to the silylation agent is SiO2: silylation reagent ═ 1: (0.01-0.06).
According to the invention, the silylating agent is preferably a compound of the general formula:
According to the present invention, the organophosphorus compound can be selected from a wide range, and for the present invention, it is preferable that the organophosphorus compound is one or more of the following formulae (II), (III) and (IV),
wherein, R in the formula (II), the formula (III) and the formula (IV) is one or more of alkyl, aryl and amido; preferably, R in the formula (II), the formula (III) and the formula (IV) is one or more of C1-C18 linear alkyl, C3-C18 branched alkyl, C6-C16 aryl and amine.
According to a preferred embodiment of the present invention, it is preferred that the organophosphorus compound is one or more of triethyl phosphate, tripropyl phosphate, tributyl phosphate, triisobutyl phosphate, trihexyl phosphate, trioctyl phosphate, tricresyl phosphate, triphenyl phosphate, and tris (2-chloropropyl) phosphate.
According to a preferred embodiment of the invention, the first part of the organophosphorus compound is triphenyl phosphate and the second part of the organophosphorus compound is tris (2-chloropropyl) phosphate.
According to the present invention, the silicon source may be a silicon source commonly used for synthesizing a silicon-containing molecular sieve, which is well known to those skilled in the art, and the present invention is not particularly limited thereto, for example, the silicon source may be at least one of silicon ester (organosilicate), solid silica gel, silica white and silica sol; in order to avoid the possible influence of the heteroatom in the silicon source, such as trivalent heteroatom like boron or aluminum, on the crystallization of the silicon-containing molecular sieve, the silicon source is preferably at least one of silicone ester, solid silica gel and white carbon black with high silicon dioxide content and low impurity content; further preferred is a silicone ester, wherein the general formula of the silicone ester is represented by the following formula (V):
in the formula (V), R1、R2、R3And R4Each is C1-C4Alkyl of (2) including C1-C4Straight chain alkyl of (2) and C3-C4Branched alkyl groups such as: r1、R2、R3And R4Each of which may be methyl, ethyl, n-propyl, isopropyl, n-butyl, sec-butyl, isobutyl or tert-butyl, with R being preferred1、R2、R3And R4Are both methyl or ethyl.
According to the method of the present invention, the silicone grease is, for example, one or more of methyl orthosilicate, ethyl orthosilicate, propyl orthosilicate, and butyl orthosilicate. Specifically, the silicone grease may be one or more of tetramethyl orthosilicate, tetraethyl orthosilicate, tetra-n-propyl orthosilicate, and tetra-n-butyl orthosilicate.
According to the invention, the structure used in step (1) isThe directing agent can be a structure directing agent commonly used in the synthesis of the silicon-containing molecular sieve, and the structure directing agent is not particularly limited in the invention, for example, the structure directing agent can be at least one of quaternary ammonium hydroxide, aliphatic amine and aliphatic alcohol amine; wherein the quaternary ammonium base can be organic quaternary ammonium base, and the aliphatic amine can be NH3Wherein at least one hydrogen is replaced by an aliphatic hydrocarbon group (e.g., alkyl), wherein the aliphatic alcohol amine can be any of various NH3Wherein at least one hydrogen is substituted with a hydroxyl-containing aliphatic group (e.g., an alkyl group).
Specifically, the structure directing agent may be at least one selected from the group consisting of a quaternary ammonium base represented by formula VI, an aliphatic amine represented by formula VII, and an aliphatic alcohol amine represented by formula VIII.
In the formula VI, R1、R2、R3And R4Each is C1-C4Alkyl of (2) including C1-C4Straight chain alkyl of (2) and C3-C4Branched alkyl groups of (a), for example: r1、R2、R3And R4Each may be methyl, ethyl, n-propyl, isopropyl, n-butyl, sec-butyl, isobutyl or/and tert-butyl.
R5(NH2)n(formula VII)
In formula VII, n is an integer of 1 or 2. When n is 1, R5Is C1-C6Alkyl of (2) including C1-C6Straight chain alkyl of (2) and C3-C6Such as methyl, ethyl, n-propyl, isopropyl, n-butyl, sec-butyl, isobutyl, tert-butyl, n-pentyl, neopentyl, isopentyl, tert-pentyl and n-hexyl. When n is 2, R5Is C1-C6Alkylene of (2) including C1-C6Linear alkylene of (A) and (C)3-C6Branched alkylene of (a) such as methylene, ethylene, n-propylene, n-butylene, n-pentylene or/andn-hexylene.
(HOR6)mNH(3-m)(formula VIII)
In the formula VIII, m are R6May be the same or different and are each C1-C4Alkylene of (2) including C1-C4Linear alkylene of (A) and (C)3-C4Branched alkylene groups of (a), such as methylene, ethylene, n-propylene and/or n-butylene; m is 1, 2 or 3.
Preferably, the structure directing agent of step (1) may be tetramethylammonium hydroxide, tetraethylammonium hydroxide, tetrapropylammonium hydroxide (including various isomers of tetrapropylammonium hydroxide, such as tetra-n-propylammonium hydroxide and tetraisopropylammonium hydroxide), tetrabutylammonium hydroxide (including various isomers of tetrabutylammonium hydroxide, such as tetra-n-butylammonium hydroxide and tetraisobutylammonium hydroxide); further, the structure directing agent is tetrapropylammonium hydroxide.
In the present invention, tetrapropylammonium hydroxide is exemplarily used as a template to illustrate the advantages of the present invention.
According to the method of the present invention, the group VIII metal source is a water-soluble group VIII metal compound; for example, when the group VIII metal is cobalt, the metal compound is one or more of cobalt trifluoride, potassium hexacyanocobaltate, sodium hexanitrocobaltate, cobalt acetylacetonate, cobalt hexacarbamate, cobalt tris (2, 4-pentanedionate), and cobalt bis (pentamethylcyclopentadienyl) hexafluorophosphate.
According to the invention, the hydrolysis conditions have no special requirements and can be conventional hydrolysis conditions in the field, and for the invention, the preferable hydrolysis conditions comprise that the molar ratio of material feeding is SiO2: structure directing agent: group VIII metal: h2O is 1: (0.001-5): (0.0001-0.1): (5-400), preferably SiO2: structure directing agent: group VIII metal: h2O＝1：(0.05-0.1)：(0.0005-0.01)：(200-400)。
According to the present invention, the conditions of the hydrolysis are not particularly critical and may be those conventional in the art, and for the purposes of the present invention, preferred conditions of the hydrolysis include a temperature of from 10 to 120 ℃, preferably from 30 to 60 ℃.
The hydrolysis time can be selected according to the hydrolysis temperature, and is generally 1-24h, preferably 4-10 h.
According to the present invention, the crystallization conditions may be conventional in the art, and preferably include: crystallizing under a closed condition at the temperature of 110-230 ℃, preferably at the temperature of 130-200 ℃.
The crystallization time can be adjusted according to time, and the crystallization time is preferably 1 to 240 hours, preferably 10 to 28 hours for the invention.
According to the method of the present invention, the hydrolysis is performed in the presence of an aqueous solvent, the kind of the aqueous solvent can be selected conventionally in the field, and various aqueous solvents can be used for implementing the present invention, wherein the amount of water in the aqueous solvent is sufficient to satisfy the condition that the silicon source generates the silicon-containing molecular sieve in the crystallization process. The solvent is preferably water, and other co-solvents may be added as needed, and are not specifically required for the present invention and will not be described in detail herein. The aqueous solvent may be derived directly from the solvent portion of the other raw material solution, for example, may be derived directly from the solvent portion of the aqueous solution of the structure directing agent; the solvent may be added directly, or if the solvent portion of the other raw material aqueous solution can satisfy the charging requirement of the aqueous solvent, the aqueous solvent is not required to be added, or if the solvent portion does not satisfy the charging requirement, the aqueous solvent is required to be additionally added.
In the present invention, the pressure for crystallization is not particularly required, and crystallization can be carried out under autogenous pressure.
According to the method of the present invention, preferably the method further comprises: and filtering and washing the crystallized product to obtain a solid, and roasting the obtained solid after drying or not drying.
In the present invention, the drying conditions can be selected in a wide range, and the drying can be specifically performed with reference to the prior art. For the present invention, it is preferable that the drying conditions include: the temperature is between room temperature and 200 ℃, and more preferably between 80 and 120 ℃; the time is 1-24h, preferably 2-10 h.
In the present invention, the optional range of the calcination conditions is wide, and for the present invention, the calcination conditions preferably include: the roasting temperature is 300-800 ℃, preferably 450-550 ℃; the roasting time is 2-12h, preferably 2-4 h.
According to the method of the present invention, the catalyst may contain the silicon-containing molecular sieve of the present invention, and the content of the silicon-containing molecular sieve of the present invention in the catalyst is preferably 50% by weight or more, more preferably 60 to 100% by weight. In the specific examples of the present invention, the catalyst containing the silicon-containing molecular sieve of the present invention in an amount of 100 wt% is used, but this does not limit the scope of the present invention. The content herein refers to the composition of the catalyst without a support.
When the catalyst is a molded body, the catalyst further comprises a carrier, wherein the carrier can be Al2O3、ZnO、MgO、SiO2CaO and TiO2Rare earth oxide RE2O3(RE is La, Ce, Y, Nd, or the like).
In the invention, besides the silicon-containing molecular sieve, the catalyst can also contain other commonly used catalysts for processing cyclohexane oxidation liquid.
According to a preferred embodiment of the present invention, the catalyst is preferably the silicon-containing molecular sieve of the present invention in an amount of 100 wt%, and the contacting conditions include: the temperature is 80-100 deg.C, preferably 85-95 deg.C.
The weight ratio of the catalyst to the cyclohexane oxidation liquid is (0.001-0.5): 1, preferably (0.01-0.2): 1, more preferably (0.02-0.1): 1.
the following examples further illustrate the invention but do not limit the scope of the invention. All reagents used in the examples were commercially available chemically pure reagents.
In the examples, water is used as the aqueous solvent, and in the mixing process, if the water contained in the other feed is sufficient for the feed of water, no water is required, and if not, water is added as necessary.
Example 1
(1) Hydrolyzing tetraethyl orthosilicate, cobalt trifluoride, tripropyl phosphate and tetrapropyl ammonium hydroxide aqueous solution (the concentration is 25 weight percent) to obtain a hydrolyzed material; the hydrolysis temperature is 30 ℃, and the hydrolysis time is 10 hours;
(2) mixing the hydrolyzed material, tripropyl phosphate and methyl triethoxysilane, and transferring the mixture to a crystallization kettle for crystallization, wherein the mixing conditions comprise: the temperature is 70 ℃, the time is 4h, and the crystallization conditions comprise: crystallizing under autogenous pressure under a closed condition, wherein the temperature is 160 ℃, and the time is 24 hours;
wherein the three propyl phosphate used in the step (1) and the step (2) respectively accounts for 30 wt% and 70 wt% of the total three propyl phosphate;
the molar ratio of each material fed is SiO2: structure directing agent: group VIII metal: h2O＝1：0.05：0.005：200，SiO2: the molar ratio of the silylation agent is 1: 0.03, P: SiO 220.1: 1;
and filtering, drying (drying at 110 ℃ for 60 minutes) and roasting (roasting at 550 ℃ for 3 hours in air atmosphere) the crystallized product to obtain the silicon-containing molecular sieve C1.
Example 2
(1) Hydrolyzing tetrapropyl orthosilicate, sodium hexanitrocobaltate, trioctyl phosphate and tetrapropyl ammonium hydroxide aqueous solution (the concentration is 25 weight percent) to obtain hydrolyzed material; the hydrolysis temperature is 50 ℃, and the hydrolysis time is 6 h;
(2) mixing the hydrolyzed material, trioctyl phosphate and phenyltriethoxysilane, and transferring the mixture to a crystallization kettle for crystallization, wherein the mixing conditions comprise: the temperature is 80 ℃, the time is 3h, and the crystallization conditions comprise: crystallizing under autogenous pressure under a closed condition, wherein the temperature is 130 ℃, and the time is 28 hours;
wherein the using amounts of the trioctyl phosphate in the step (1) and the step (2) are respectively 35 wt% and 65 wt% of the total using amount of the trioctyl phosphate;
the molar ratio of each material fed is SiO2: structure directing agent: group VIII metal: h2O＝1：0.06：0.008：300，SiO2: the molar ratio of the silylation agent is 1: 0.05, P: SiO 220.2: 1;
and filtering, drying (drying at 110 ℃ for 60 minutes) and roasting (roasting at 550 ℃ for 3 hours in air atmosphere) the crystallized product to obtain the silicon-containing molecular sieve C2.
Example 3
(1) Hydrolyzing tetra-n-butyl orthosilicate, cobalt tris (2, 4-pentanedionate), tris (2-chloropropyl) phosphate and tetrapropyl ammonium hydroxide aqueous solution (with the concentration of 25 weight percent) to obtain a hydrolyzed material; the hydrolysis temperature is 60 ℃, and the hydrolysis time is 4 hours;
(2) mixing the hydrolyzed material, tris (2-chloropropyl) phosphate and hexamethyldisilazane, and transferring the mixture to a crystallization kettle for crystallization, wherein the mixing conditions comprise: the temperature is 90 ℃, the time is 2h, and the crystallization conditions comprise: crystallizing under autogenous pressure under a closed condition at the temperature of 200 ℃ for 10 hours;
wherein the using amounts of the trioctyl phosphate in the step (1) and the step (2) are respectively 40 wt% and 60 wt% of the total using amount of the trioctyl phosphate;
the molar ratio of each material fed is SiO2: structure directing agent: group VIII metal: h2O＝1：0.1：0.01：400，SiO2: the molar ratio of the silylation agent is 1: 0.04, P: SiO 220.3: 1;
and filtering, drying (drying at 110 ℃ for 60 minutes) and roasting (roasting at 550 ℃ for 3 hours in air atmosphere) the crystallized product to obtain the silicon-containing molecular sieve C3.
Example 4
A silicaceous molecular sieve C4 was prepared according to the method of example 1, except that the total amount of tripropyl phosphate was added in step (1).
Example 5
A silicaceous molecular sieve C5 was prepared according to the method of example 1, except that the total amount of tripropyl phosphate was added in step (2).
Example 6
A silicaceous molecular sieve C6 was prepared according to the method of example 1, except that methyltriethoxysilane was added in step (1).
Example 7
A silicaceous molecular sieve C7 was prepared according to the method of example 1, except that the mixing temperature in step (2) was 60 ℃ for 10 hours.
Example 8
A silicaceous molecular sieve C8 was prepared according to the method of example 1, except that the mixing temperature in step (2) was 100 ℃ for 1 h.
Example 9
A silicaceous molecular sieve C9 was prepared in accordance with the procedure of example 1, except that the amount of tripropyl phosphate used in step (1) and step (2) was 70% by weight and 30% by weight, respectively, of the total amount of tripropyl phosphate used.
Example 10
A silicaceous molecular sieve C10 was prepared in accordance with the procedure of example 1, except that the amount of tripropyl phosphate used in step (1) and step (2) was 20 wt% and 80 wt%, respectively, of the total amount of tripropyl phosphate used.
Example 11
A silicaceous molecular sieve C11 was prepared according to the method of example 1, except that P: SiO 220.4: 1.
example 12
A silicon-containing molecular sieve C12 was prepared by the method of example 1, except that the organophosphorus compound in step (1) was triphenyl phosphate and the organophosphorus compound in step (2) was tris (2-chloropropyl) phosphate.
Example 13
A silicaceous molecular sieve C13 was prepared according to the method of example 1, except that the group VIII metal compound was nickel nitrate.
Example 14
A silicaceous molecular sieve C14 was prepared according to the procedure described in example 1, except that the silylating agent was tert-butyldimethylsilyl chloride.
Test example
The test example is used to illustrate the reaction effect of the silicon-containing molecular sieve obtained by the method of the present invention and the silicon-containing molecular sieve obtained by the method of the comparative example on the cyclohexane oxidation liquid processing reaction.
The samples prepared in the above examples 1 to 14 and comparative example 1 were used for catalyzing the decomposition of cyclohexane oxidation liquid, and the cyclohexane oxidation liquid was contacted with the catalyst at 85 ℃ for 2 hours, wherein the weight ratio of the catalyst to the cyclohexane oxidation liquid was 0.01: 1, results are shown in table 1 below.
Wherein, the cyclohexane oxidation liquid is an industrial product which is decomposed without catalytic oxidation at 160 ℃, and the cyclohexane oxidation liquid specifically comprises the following components: 3.5% by weight of cyclohexyl hydroperoxide, 0.7% by weight of cyclohexanol, 0.5% by weight of cyclohexanone, 0.20% by weight of organic acid, 0.30% by weight of organic ester, 94.8% by weight of cyclohexane.
The product obtained was, among others, subjected to an Agilent6890N chromatograph using an HP-5 capillary column (30 m.times.0.25 mm) to determine the distribution of the individual products.
Cyclohexyl hydroperoxide conversion (%) — moles of cyclohexyl hydroperoxide participating in the reaction/moles of cyclohexyl hydroperoxide added.
Alcohol-ketone selectivity (%) (the number of moles of cyclohexanone in the reaction solution + the number of moles of cyclohexanol in the reaction solution-the number of moles of cyclohexanone in the oxidation solution-the number of moles of cyclohexanol in the oxidation solution)/the number of moles of cyclohexyl hydroperoxide participating in the reaction.
The ratio of alcohol to ketone (mole number of cyclohexanol in reaction solution-mole number of cyclohexanol in oxidation solution)/(mole number of cyclohexanone in reaction solution-mole number of cyclohexanone in oxidation solution)
Wherein the number of moles of cyclohexylhydroperoxide participating in the reaction is equal to the number of moles of cyclohexylhydroperoxide charged into the oxidation liquid — the number of moles of cyclohexylhydroperoxide remaining in the obtained reaction liquid.
TABLE 1
From the results in table 1, it can be seen that the silicon-containing molecular sieve prepared by the method of the present invention has high catalytic activity, and the cobalt-containing molecular sieve is used for catalytic decomposition of cyclohexane oxidation liquid, and can obtain more than 99% of cyclohexyl hydroperoxide conversion rate and more than 95% of alcohol ketone selectivity within 2h at 85 ℃.
The preferred embodiments of the present invention have been described in detail, however, the present invention is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are within the protective scope of the present invention.
Claims (19)
1. A method for processing cyclohexane oxide liquid, which comprises the following steps: contacting cyclohexane oxidation liquid with a catalyst, wherein the cyclohexane oxidation liquid contains cyclohexyl hydrogen peroxide, the catalyst contains a silicon-containing molecular sieve, and the preparation method of the silicon-containing molecular sieve comprises the following steps:
(1) hydrolyzing a silicon source, a VIII group metal source and a structure directing agent to obtain a hydrolyzed material;
(2) crystallizing the hydrolyzed material;
wherein, the step (1) is carried out in the presence of an organic phosphorus compound and/or before the step (2), the hydrolyzed material is mixed with the organic phosphorus compound and then the crystallization is carried out;
the cyclohexane oxidation liquid contains cyclohexyl hydrogen peroxide, cyclohexanol, cyclohexanone and cyclohexane; the cyclohexane oxidation liquid contains 3.0-3.6 wt% of cyclohexyl hydrogen peroxide, 0.6-1.0 wt% of cyclohexanol, 0.4-0.7 wt% of cyclohexanone, 0.15-0.3 wt% of organic acid, 0.2-0.4 wt% of organic ester and 94.00-95.65 wt% of cyclohexane;
the conditions for contacting the cyclohexane oxidation liquid with the catalyst include: the temperature is 80-100 ℃;
the weight ratio of the catalyst to the cyclohexane oxidation liquid is (0.001-0.5): 1;
the content of the silicon-containing molecular sieve in the catalyst is more than 50 weight percent;
the molar ratio of the organophosphorus compound to the silicon source is P: SiO 22＝(0.001-0.5)：1。
2. The method of claim 1, wherein,
the cyclohexane oxidation liquid is an industrial product without catalytic oxidation;
the conditions for contacting the cyclohexane oxidation liquid with the catalyst include: the temperature is 85-95 ℃;
the weight ratio of the catalyst to the cyclohexane oxidation liquid is (0.01-0.2): 1;
the content of the silicon-containing molecular sieve in the catalyst is 60-100 wt%;
the molar ratio of the organophosphorus compound to the silicon source is P: SiO 22＝(0.1-0.3)：1。
3. The process according to claim 2, wherein the weight ratio of catalyst to cyclohexane oxidation liquid is (0.02-0.1): 1.
4. the method of claim 1, wherein the method of making comprises:
(1) hydrolyzing a silicon source, a VIII group metal source, a first part of organic phosphorus compound and a structure directing agent to obtain a hydrolyzed material;
(2) and mixing the hydrolyzed material with a second part of organic phosphorus compound, and then carrying out crystallization.
5. The process of claim 4 wherein the first portion of organophosphorus compounds is present in an amount of 10 to 90 wt.% and the second portion of organophosphorus compounds is present in an amount of 10 to 90 wt.%, based on 100 wt.% of the total amount of organophosphorus compounds.
6. The process of claim 5 wherein the first portion of organophosphorus compound is present in an amount of 30 to 40 wt.% and the second portion of organophosphorus compound is present in an amount of 60 to 70 wt.%, based on 100 wt.% of the total amount of organophosphorus compounds.
7. The method of claim 1, wherein the conditions under which the hydrolyzed material is mixed with the organophosphorus compound comprise: the temperature is 60-100 ℃, and/or the time is 1-10 h.
8. The method of claim 7, wherein the conditions under which the hydrolyzed material is mixed with the organophosphorus compound comprise: the temperature is 70-90 ℃ and/or the time is 2-4 h.
9. The method of claim 1, wherein the group VIII metal is one or more of cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium, and platinum.
10. The method of claim 1, wherein the group VIII metal is cobalt.
11. The process of claim 1, wherein hydrolyzing a silicon source, a group VIII metal source, and a structure directing agent is carried out in the presence of a silylating agent and/or mixing the hydrolyzed material with an organophosphorus compound is carried out in the presence of a silylating agent; the molar ratio of the silicon source to the silanization reagent is SiO2: silylation reagent ═ 1: (0.001-0.1); the silanization reagent is a compound with the following general formula (I):
12. The method of claim 11, wherein the molar ratio of the silicon source to the silylating agent is SiO2: silylation reagent ═ 1: (0.01-0.06).
13. The method of claim 11, wherein the silylating agent is at least one of dimethyldichlorosilane, methyltrichlorosilane, trimethylchlorosilane, 1, 7-dichlorooctylmethyltetrasiloxane, [ 3-trimethoxysilylpropyl ] dimethyloctadecylammonium bromide, N-phenyl-3-aminopropyltrimethoxysilane, phenyltriethoxysilane, hexamethyldisilazane, hexamethyldisiloxane, methyltriethoxysilane, t-butyldimethylchlorosilane, hexadecyltrimethoxysilane, and octyltriethoxysilane.
14. The method of claim 11, wherein the silylating agent is at least one of phenyltriethoxysilane, hexamethyldisilazane, hexamethyldisiloxane, and methyltriethoxysilane.
15. The method of claim 11, wherein the method of making comprises:
(1) hydrolyzing a silicon source, a VIII group metal source, a first part of organic phosphorus compound and a structure directing agent to obtain a hydrolyzed material;
(2) mixing the hydrolyzed material, a second part of organic phosphorus compound and a silanization reagent and then carrying out crystallization;
the total dosage of the organic phosphorus compounds is 100 weight percent, the dosage of the first part of organic phosphorus compounds is 10 to 90 weight percent, the dosage of the second part of organic phosphorus compounds is 10 to 90 weight percent, and the molar ratio of the silicon source to the silanization reagent is SiO2: silylation reagent ═ 1: (0.001-0.1).
16. The method of claim 15 wherein the first portion of the organophosphorus compound is present in an amount of 30 to 40 wt% and the second portion of the organophosphorus compound is present in an amount of 60 to 70 wt%, based on 100 wt% of the total amount of organophosphorus compounds, and the molar ratio of the silicon source to the silylating agent is SiO2: silylation reagent ═ 1: (0.01-0.06).
17. The method of any one of claims 1-16,
the organophosphorus compound is one or more of the following formulas (II), (III) and (IV),
wherein, R in the formula (II), the formula (III) and the formula (IV) is one or more of alkyl, aryl and amido;
r in the formula (II), the formula (III) and the formula (IV) is one or more of C1-C18 straight-chain alkyl, C3-C18 branched-chain alkyl, C6-C16 aryl and amine;
the silicon source is at least one selected from methyl orthosilicate, ethyl orthosilicate, propyl orthosilicate, butyl orthosilicate, silica gel, white carbon black and silica sol;
the structure directing agent is at least one selected from fatty amine, alcohol amine and quaternary ammonium base compounds;
the VIII family metal source is water-soluble VIII family metal compound, and the water-soluble VIII family metal compound is one or more of cobalt trifluoride, potassium hexacyanocobaltate, sodium hexanitrocobaltate, cobalt acetylacetonate, cobalt hexacarbamate, cobalt tris (2, 4-pentanedionate) and cobalt bis (pentamethylcyclopentadienyl) hexafluorophosphate;
the hydrolysis condition comprises that the molar ratio of the materials is SiO2: structure directing agent: group VIII metal: h2O is 1: (0.001-5): (0.0001-0.1): (5-400) the temperature is 10-120 ℃, and the time is 1-24 h;
the crystallization conditions include: crystallizing under sealed condition at 110-230 deg.C and/or for 1-240 hr.
18. The method of claim 17 wherein the organophosphorus compound is one or more of triethyl phosphate, tripropyl phosphate, tributyl phosphate, triisobutyl phosphate, trihexyl phosphate, trioctyl phosphate, tricresyl phosphate, triphenyl phosphate, and tris (2-chloropropyl) phosphate.
19. The method of claim 17, wherein the structure directing agent is at least one selected from the group consisting of tetramethylammonium hydroxide, tetraethylammonium hydroxide, tetrapropylammonium hydroxide, and tetrabutylammonium hydroxide.
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