CN102218326B - Oxide catalyst for producing Alpha-Alpha-dimethylphenyl carbinol and preparation method thereof - Google Patents

Abstract

The invention relates to an oxide catalyst for producing Alpha-Alpha-dimethylphenyl carbinol and a preparation method thereof, and mainly solves the technical problem that a product contents sulphur when sodium sulfide and sodium sulfite are used as reducers in the prior art. The oxide catalyst comprises the following components by weight percentage: 30-90% of manganese oxide, 0.1-10% of at least one oxide out of copper, cobalt or iron, 0.1-10% of at least one oxide out of alkali metal oxides, and 5-60% of alumina carriers. The technical scheme for preparing the catalyst and a corresponding preparation method better solves the problem and can be applied to the industrial production of the Alpha-Alpha-dimethylphenyl carbinol.

Description

For the production of α, oxide catalyst of alpha-alpha-dimethyl benzylalcohol and preparation method thereof

Technical field

The present invention relates to a kind of for the production of α, oxide catalyst of alpha-alpha-dimethyl benzylalcohol and preparation method thereof.

Background technology

α, (be called for short: be a kind of important organic intermediate DMPC), (be called for short: CHP) reaction preparation cumyl peroxide (is called for short: DCP) alpha-alpha-dimethyl benzylalcohol to be mainly used in same hydrogen phosphide cumene.The at present preparation of DMPC all prepares take CHP as raw material and obtains, the method of producing Organic Alcohol take organic peroxide as raw material mainly is to adopt the inorganic reducing agent reducing process, use the method [US 2484841-1949] of inorganic reducing agent with inorganic salts and the peroxide reactions of equivalent, generate the inorganic acid salt of a large amount of waste water and cheapness, cause serious environmental pollution.Present production method mainly adopts this type, with Na ₂S or Na ₂SO ₃The aqueous solution be reducing agent, and the CHP of equivalent reacts between 80～100 ℃, the reaction time is 2～6 hours, the conversion ratio of CHP about 96%, DMPC selectively about 95%; Although the reaction afterproduct through separation, rectifying, but still contain a certain amount of sulphur, not only affected the quality of product but also affected follow-up separating technology; Owing to containing a large amount of water in the reaction system, thereby having caused the loss of CHP and DMPC, having reduced productive rate.And take composite metal oxide as catalyst, adopt the liquid and solid phase reaction system, the oxidisability of organic peroxide and the reproducibility of solvent have not only effectively been utilized, and product easily separates with catalyst, take oxidation-coupling principle as guidance, can produce the Organic Alcohol greater than the metering ratio, and the selective height of Organic Alcohol, the content of ketone, aldehyde is low, and catalyst active high can be at room temperature reaction.

Summary of the invention

One of technical problem to be solved by this invention is to have preparation α in the prior art, in the process of alpha-alpha-dimethyl benzylalcohol with Na ₂S or Na ₂SO ₃Solution when being reducing agent, reaction temperature is high, α, alpha-alpha-dimethyl benzylalcohol yield is low, CHP and α, alpha-alpha-dimethyl benzylalcohol runs off, and contains the problem of sulphur in product and the waste liquid, provide a kind of newly for the production of α, the oxide catalyst of alpha-alpha-dimethyl benzylalcohol.This catalyst has high catalytic activity and selective advantage for the production of α during alpha-alpha-dimethyl benzylalcohol.Two of technical problem to be solved by this invention provides a kind of preparation method of the catalyst corresponding with one of technical solution problem.

In order one of to solve the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of for the production of α, the oxide catalyst of alpha-alpha-dimethyl benzylalcohol comprises following component by weight percentage:

A) oxide of 30～90% manganese;

B) 0.1～10% at least a oxide that is selected from copper, cobalt or the iron;

C) 0.1～10% be selected from least a in the alkali metal oxide;

D) 5～60% alumina support.

In the technique scheme, manganese source preferred version is selected from least a in potassium permanganate, potassium manganate, manganese nitrate or the manganese dioxide; Aluminium source preferred version is selected from least a in boehmite, aluminium oxide or the aluminium colloidal sol; Copper source preferred version is selected from least a in copper nitrate, cupric oxalate, copper carbonate, Kocide SD or the cupric tetramminohydroxide; Cobalt source preferred version is selected from least a in cobalt nitrate or the cobalt oxide; The source of iron preferred version is selected from least a in ferric nitrate or the iron oxide; The alkali metal oxide preferred version is selected from least a in sodium oxide molybdena or the potassium oxide; Carrier is aluminium oxide.The specific area preferred version of catalyst is 10～100m ²/ g, total pore volume is 0.01～0.5 ml/g.

For solve the problems of the technologies described above two, the technical solution used in the present invention is as follows: a kind of for the production of α, the preparation method of the oxide catalyst of alpha-alpha-dimethyl benzylalcohol may further comprise the steps:

1) with the KMnO of aequum ₄Solution places reactor, and adds the nitric acid of aequum;

2) with the Mn (NO of aequum ₃) ₂Co (the NO of solution and aequum ₃) ₂, Cu (NO ₃) ₂Or Fe (NO ₃) ₂And composition thereof solution mix;

3) with 1) with 2) under room temperature, mix, and transfer in the autoclave in 80～150 ℃ of constant temperature 50～240 hours;

4) with 3) resulting product filters, washing and rear in 80～150 ℃ of oven dry with the nitric acid washing;

5) with 4) resulting product mixes with the aluminium oxide of aequum, extruded moulding, roasting gets required catalyst.

The present invention proposes a kind of a kind of for the production of α of prior art that be different from, oxide catalyst of alpha-alpha-dimethyl benzylalcohol and preparation method thereof obtains a kind of manganese-base oxide catalyst by above-mentioned technical scheme, and specific area is at 10～100 meters ²/ gram, total pore volume is at 0.01～0.5 ml/g.Because catalyst has suitable acidity, and CHP is had very high catalytic activity, has reduced significantly the decomposition temperature of CHP, has reduced thermal decomposition product, relatively improved the selective of DMPC (α, alpha-alpha-dimethyl benzylalcohol); And the moderate oxidation-reduction quality of catalyst has effectively utilized the elemental oxygen that generates in the CHP decomposable process, and cumene oxidation is to DMPC, so that the productive rate of DMPC is higher than theoretical yield cheaply.

Catalyst of the present invention has good acidity and distributes and oxidation-reduction quality, when catalysis CHP decomposes again can with isopropylbenzene cheaply partly change into DMCP; Because it is appropriate that reaction temperature is low and the active sites of catalyst distributes, and can effectively avoid the thermal decomposition of CHP; Because catalyst has the oxidation-reduction quality of appropriateness, thus in the product take DMPC as main, and the by-products contents such as acetophenone, methyl styrene are few; Because catalyst has the acidity of appropriateness, so avoided the reaction of sour decomposition, does not have phenol and acetone in the product after this catalytic reaction.Catalyst of the present invention is produced α being used for catalytic decomposition CHP, during alpha-alpha-dimethyl benzylalcohol, when CHP mass concentration during at 1～70wt%, reaction temperature at 10～100 ℃, reaction pressure in 0.1～1 MPa, liquid phase air speed at 0.1～6 hour ^-1Condition under, DMPC one way weight selectively is up to 97.5%, the weight content of acetophenone, methyl styrene is below 3%, the conversion ratio of CHP has been obtained preferably technique effect more than 99%.

The invention will be further elaborated below by embodiment, but these embodiment in no case are construed as limiting scope of the present invention.

The specific embodiment

[embodiment 1]

Under room temperature, take by weighing respectively 126.4g KMnO ₄, 20.2g Fe (NO ₃) ₃9H ₂O, 2.41gCu (NO ₃) ₂, 8.76gCo (C ₂O ₄) ₂2H ₂O, and above-claimed cpd is dissolved in the 1.0L deionized water, then in mentioned solution, add red fuming nitric acid (RFNA), regulate about pH to 1.0, take by weighing simultaneously the Mn (NO of 22.3g ₃) ₂And join in the mentioned solution, and stir, refluxed 6 hours; Then use dense HNO ₃PH value to 8.0 with NaOH conditioned reaction system, the mixture of gained is transferred to autoclave, in 150 ℃ of constant temperature 48 hours, with resulting product behind the constant temperature filter, washing, oven dry, then the product with oven dry soaked in the nitric acid of 1mol/L 1～8 hour, again filtered thereafter, dried; And in nitrogen atmosphere in 400 ℃ of roastings 4～24 hours, get catalyst precursor I.Catalyst precursor I is mixed according to 10: 1 ratio of weight ratio with alumina powder, add an amount of nitric acid, extruded moulding gets the catalyst final products.

Get the 10mL finished catalyst, place fixed bed reactors, the temperature of reaction bed is controlled at 70 ℃, and reaction pressure maintains 0.1～1.0MPa, and the CHP of 21.8wt% is flow through catalyst with the flow velocity of 60mL/hr, and efflux adopts gas chromatographic analysis.

[embodiment 2～10]

According to embodiment 1 each Step By Condition Kaolinite Preparation of Catalyst and examination catalyst, the synthesis conditions such as kind, raw material proportioning, synthesis condition, roasting condition and shaping of catalyst factor of feed change only, and synthesis condition listed in table 1; Under same examination condition, the resulting catalyst of different synthetic methods is checked and rated, appraisal result is listed in the table 2.

Table 1

Title	Raw material type	Catalyst forms	Synthetic method+roasting condition+moulding
				Embodiment 1	KMnO 4+Fe(NO 3) 3+Co(NO 3) 2 +Cu(NO 3) 2+Mn(NO 3) 2	80% manganese oxide, 10% iron oxide, 0.1% cupric oxide, 0.1% cobalt oxide, 0.8% sodium oxide molybdena, 9% aluminium oxide	PH=3.0, air+180 ℃+aluminium oxide
Embodiment 2	K 2MnO 4+Fe(NO 3) 3+Co(C 2O 4) 2 +Cu(NO 3) 2+Mn(NO 3) 2	80% manganese oxide, 1% iron oxide, 1% cupric oxide, 1% cobalt oxide, 2% sodium oxide molybdena, 15% aluminium oxide	PH=1.0, air+240 ℃+aluminium colloidal sol
				Embodiment 3	Mn(NO 3) 2+FeCl 3+CoO+CuCl 2 +(NO 3) 2	80% manganese oxide, 10% iron oxide, 1% sodium oxide molybdena, 9% aluminium oxide	PH=4.0, air+360 ℃+aluminium oxide
Embodiment 4	(NO 3) 2+FeCl 2+Co(Ac) 2+CuO	80% manganese oxide, 10% cupric oxide, 1% sodium oxide molybdena, 9% aluminium oxide	PH=3.0, air+180 ℃+aluminium oxide
				Embodiment 5	MnO 2+Fe(NO 3) 3+Co(NO 3) 2 +Cu(NO 3) 2	70% manganese oxide, 10% cobalt oxide, 3% sodium oxide molybdena, 17% aluminium oxide	PH=6.0, air+480 ℃+boehmite
Embodiment 6	KMnO 4+Fe(NO 3) 3+Co(C 2O 4) 2 +CuSO 4+(NO 3) 2	5% sodium oxide molybdena, 20% aluminium oxide, 70% manganese oxide, 5% cobalt oxide,	PH=10.0, nitrogen+120 ℃+aluminium colloidal sol
				Embodiment 7	KMnO 4+Fe(NO 3) 3+Co(Ac) 2 +CuCl 2	60% manganese oxide, 5% iron oxide, 5% potassium oxide, 30% aluminium oxide	PH=9.0, air+270 ℃+aluminium oxide
Embodiment 8	MnO 2+Fe(NO 3) 3+Co(C 2O 4) 2 +Cu(NO 3) 2	60% manganese oxide, 5% cupric oxide, 1% potassium oxide, 34% aluminium oxide	PH=4.0, air+560 ℃+aluminium oxide
				Embodiment 9	K 2MnO 4+Fe 2(SO 4) 3+Co(NO 3) 2 +Cu(NO 3) 2	50% manganese oxide, 1% cobalt oxide, 10% sodium oxide molybdena, 39% aluminium oxide	PH=6.0, nitrogen+200 ℃+aluminium colloidal sol
Embodiment 10	K 2MnO 4+Fe(NO 3) 3+Co(Ac) 2 +Cu(NO 3) 2	30% manganese oxide, 1% iron oxide, 10% sodium oxide molybdena, 59% aluminium oxide	PH=12.0, air+600 ℃+aluminium colloidal sol

Table 2

Claims (4)

1. one kind for the production of α, and the oxide catalyst of alpha-alpha-dimethyl benzylalcohol comprises following component by weight percentage:

A) oxide of 30～90% manganese;

B) 0.1～10% at least a oxide that is selected from copper, cobalt or the iron;

C) 0.1～10% be selected from least a in the alkali metal oxide;

D) 5～60% alumina support;

The preparation method of described oxide catalyst may further comprise the steps:

1) with the KMnO of aequum ₄Solution places reactor, and adds the nitric acid of aequum;

2) with the Mn (NO of aequum ₃) ₂Co (the NO of solution and aequum ₃) ₂, Cu (NO ₃) ₂Or Fe (NO ₃) ₂And composition thereof solution mix;

3) with 1) with 2) under room temperature, mix, and transfer in the autoclave in 80～150 ℃ of constant temperature 50～240 hours;

4) with 3) resulting product filters, washing and rear in 80～150 ℃ of oven dry with the nitric acid washing;

5) with 4) resulting product mixes with the aluminium oxide of aequum, extruded moulding, roasting gets required catalyst.

2. described for the production of α according to claim 1, the oxide catalyst of alpha-alpha-dimethyl benzylalcohol is characterized in that the manganese source is selected from least a in potassium permanganate, potassium manganate, manganese nitrate or the manganese dioxide; The aluminium source is selected from least a in boehmite, aluminium oxide or the aluminium colloidal sol; The copper source is selected from least a in copper nitrate, cupric oxalate, copper carbonate, Kocide SD or the cupric tetramminohydroxide; Cobalt is derived from least a in cobalt nitrate or the cobalt oxide; Source of iron is selected from least a in ferric nitrate or the iron oxide; Alkali metal oxide is selected from least a in sodium oxide molybdena or the potassium oxide; The oxide consumption of manganese is 30～60% by weight percentage, and at least a oxide consumption that is selected from copper, cobalt or the iron is 1～6%, and at least a consumption that is selected from the alkali metal oxide is 1～10%, and the consumption of alumina support is 20～60%.

3. described for the production of α according to claim 1, the oxide catalyst of alpha-alpha-dimethyl benzylalcohol, the specific area that it is characterized in that catalyst is 10～100m ²/ g, total pore volume is 0.01～0.5 ml/g.

4. described for the production of α according to claim 1, the preparation method of the oxide catalyst of alpha-alpha-dimethyl benzylalcohol may further comprise the steps:

1) with the KMnO of aequum ₄Solution places reactor, and adds the nitric acid of aequum;

2) with the Mn (NO of aequum ₃) ₂Co (the NO of solution and aequum ₃) ₂, Cu (NO ₃) ₂Or Fe (NO ₃) ₂And composition thereof solution mix;

3) with 1) with 2) under room temperature, mix, and transfer in the autoclave in 80～150 ℃ of constant temperature 50～240 hours;

4) with 3) resulting product filters, washing and rear in 80～150 ℃ of oven dry with the nitric acid washing;

5) with 4) resulting product mixes with the aluminium oxide of aequum, extruded moulding, roasting gets required catalyst.