CN101786947A - Method for preparing benzaldehyde by oxidizing toluene - Google Patents
Method for preparing benzaldehyde by oxidizing toluene Download PDFInfo
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Abstract
The invention relates to a method for preparing benzaldehyde by oxidizing toluene. Currently, no method for producing the benzaldehyde has simple reactions as well as high toluene percent conversion and benzaldehyde selectivity. The raw materials comprise 1-59% of toluene, 0.005-5% of master catalyst, oxygen source and 40-98% of benzyl benzoate, wherein the mol ratio of oxygen molecules in the oxygen source to toluene is (0.3-3):1, and the master catalyst is one or more than two of cobalt ions, manganese ions, vanadium ions and nickel ions. The method comprises the following steps: mixing the toluene, master catalyst and benzyl benzoate in a reactor; at the temperature of 140-300 DEG C and under the absolute pressure of 0.05-1.0 MPa, introducing the oxygen source into the mixed liquor to react for more than 2 hours; and refining the mixed liquor to obtain the benzaldehyde. The toluene percent conversion is higher than 30%, and the benzaldehyde selectivity is higher than 70%. The invention has the advantages of simple reaction, energy conservation, environmental protection, easy separation of products and solvent, and high toluene percent conversion and benzaldehyde selectivity.
Description
Technical field
The present invention relates to a kind of preparation method of benzaldehyde, especially relate to a kind of method of preparing benzaldehyde by oxidizing toluene.
Background technology
Phenyl aldehyde is a kind of important fine chemical product, is widely used in the industrial circles such as medicine, dyestuff, spices, agricultural chemicals and material.The production method of present disclosed preparation phenyl aldehyde mainly contains following three kinds: chlorination toluene hydrolysis method, phenylformic acid (ester) reduction method and toluene direct oxidation method, wherein the toluene direct oxidation method comprises vapor phase process and liquid phase method.
Inevitably contain chlorine in the phenyl aldehyde of producing by traditional chlorination toluene hydrolysis method, and the phenyl aldehyde that is used in the industries such as medicine and spices can not contain chlorine, therefore the range of application of the phenyl aldehyde that produces by the chlorination toluene hydrolysis method has been subjected to certain restriction, the U.S. that as the patent No. is US4229379 and US2816144 produces phenyl aldehyde by the chlorination toluene hydrolysis method, this method more disadvantageously can produce a large amount of waste water in process of production, and the processing of these waste water is very difficult, thereby caused bigger threat to environment.
Phenylformic acid (ester) reduction method is meant by phenylformic acid or benzoic ether and generates method of benzaldehyde by catalytic hydrogenating reduction, though the transformation efficiency of this method and selectivity are all very high, as being described in the United States Patent (USP) of US4987265 in the patent No., transformation efficiency can reach 100% under the excessive greatly situation of hydrogen, and the selectivity of phenyl aldehyde also can reach 95%; Be that the selectivity of phenyl aldehyde can reach 95.63% described in the Chinese patent of CN101456798 in the patent No..In the patent No. is in the Chinese patent of CN1271717, discloses a kind of method by benzoic ether hydrogenation synthesizing benzaldehyde, and the per pass conversion of this method reaches 98%, and the selectivity of phenyl aldehyde reaches 87.5%.In the patent No. is in the Chinese patent of CN1876616, and the selectivity of phenyl aldehyde reaches 99% in the disclosed gas phase hydrogenation method, and yield can reach more than 95%.But the temperature of reaction of phenylformic acid (ester) reduction method must be more than 300 ℃, and energy consumption is very big; Industrial, phenylformic acid is substantially all produced by toluene oxidation, if produce benzoic ether then also need further esterification, and being exactly toluene oxidation originally, phenyl aldehyde produced benzoic intermediate product, be after toluene oxidation generates phenyl aldehyde, phenyl aldehyde continues oxidation again and generates phenylformic acid, and phenylformic acid is again by going back the original production phenyl aldehyde, thereby improved production cost greatly, caused the uneconomical of this production method ten minutes.
Toluene direct oxidation under gas phase or liquid-phase condition generates the method that phenyl aldehyde is comparatively economy and environmental protection.As far back as the patent No.s in 1919 was in the United States Patent (USP) of US1321959, disclose a kind of method of gas phase oxidation of toluene producing benzaldehyde, the temperature of reaction of this method is 500-700 ℃, but in this patent, do not provide transformation efficiency and related data optionally, it is reported, a large amount of carbon dioxide generating is arranged in above-mentioned reaction process, the problem that has over oxidation is described.After this, though the gas phase direct oxidation method has development, make progress comparatively slow.The patent No.s in 1993 was in the Chinese patent of CN1068755, disclosed a kind ofly to prepare method of benzaldehyde by gas phase oxidation of toluene, and the selectivity of the phenyl aldehyde that is prepared from by this method reaches 60%, and the once through yield of phenyl aldehyde can reach 16%.Mainly there is the temperature of reaction height in toluene by the method for vapor phase process direct oxidation, the defective of the easy over oxidation of toluene, and the selectivity of phenyl aldehyde descends comparatively obvious when improving transformation efficiency.
The patent No. in nineteen sixty-eight is in the United States Patent (USP) of US3387036, the method of a kind of toluene liquid-phase oxidation producing benzaldehyde and phenylcarbinol is disclosed, this reaction is to carry out under 170-220 ℃ in temperature, the transformation efficiency of phenyl aldehyde has only 10% at most in this method, and the selectivity of phenyl aldehyde is not high yet.The patent No.s in 2002 was in the United States Patent (USP) of US6495726 and the patent No. in 2004 to be in the United States Patent (USP) of US6743952, all reported in the organic acid medium, under 60-130 ℃ temperature, with the cobalt salt is the method that Primary Catalysts carries out liquid phase catalytic oxidation toluene, transformation efficiency at toluene is under the situation of 15-25%, and the selectivity of phenyl aldehyde is 40-50%.In the patent No. of calendar year 2001 is to gather in the Chinese patent of CN1296937 and at the Chinese patent that the patent No. in 2004 is CN1522996, all disclose and prepared method of benzaldehyde by liquid phase oxidation, this method adopts a kind of special bromide as promotor, and the selectivity of phenyl aldehyde has only about 20%.The patent No.s in 2004 was in the patent of CN1485131, the method that a kind of toluene liquid-phase oxidation prepares phenyl aldehyde and phenylcarbinol is disclosed, under solvent-free situation, the temperature of catalyzed reaction is 180-195 ℃, the pressure of reaction is 0.8-1.2MPa, transformation efficiency at toluene is 13% o'clock, and the overall selectivity of phenyl aldehyde and phenylcarbinol is 86.6%.The patent No.s in 2005 was in the Chinese patent of CN1663941, disclosed a kind of method by toluene liquid-phase oxidation producing benzaldehyde, and the temperature of this reaction is 90-160 ℃, was 10% o'clock at the transformation efficiency of toluene, and the selectivity of phenyl aldehyde reaches 62%.The patent No. in 2007 was in the United States Patent (USP) of US7189882, had reported in acetic aid medium, and when temperature is 70-180 ℃ and pressure when being 1-80bar, when the transformation efficiency of toluene was not higher than 25%, the selectivity of phenyl aldehyde reached 60-75%.The patent No.s in 2008 was in the United States Patent (USP) of US7411099, and the selectivity of the phenyl aldehyde of report reaches 76%.The patent No.s in 2009 was in the Chinese patent of CN101607867, adopted the placed in-line method of multi-stage oxidizing reactor and gas-liquid separator, toluene conversion has reached more than 95%, and the overall selectivity of phenyl aldehyde and phenylcarbinol reaches more than 50%, but the transformation efficiency of single-stage reactor is low, the energy consumption height.Above-mentionedly prepare in the method for benzaldehyde by the direct liquid phase oxidation of toluene, all can not satisfy guarantee the toluene high conversion in, guarantee that phenyl aldehyde has highly selective; Though adopt organic acid that situation is taken on a new look to some extent, increased sepn process and introduced other impurity.
The patent No.s in 2004 was in the Chinese patent of CN1528726, disclose a kind of in acidity or neutral ion liquid and acetic acid mixed solvent, prepare method of benzaldehyde by liquid-phase oxidation aromatic hydrocarbons side chain, at 115-120 ℃ of following oxidation toluene, when the transformation efficiency of toluene is 42%, the selectivity of phenyl aldehyde is 48%, the selectivity of phenylcarbinol acetic ester is 58%, this method is used a large amount of expensive ionic liquid and acetate solvates, improved production cost greatly, and product separation is comparatively difficult, the market of produced simultaneously phenylcarbinol acetic ester is little, need further to handle to reclaim phenylcarbinol and acetic acid, industrial production is uneconomical.
In sum, also there is not a kind of reaction simple at present, energy-conserving and environment-protective, product and solvent are easily separated and reclaim the production method of benzaldehyde that toluene conversion in the reaction and phenyl aldehyde selectivity are simultaneously higher.
Summary of the invention
The objective of the invention is to overcome above shortcomings in the prior art, and provide a kind of reaction simple, energy-conserving and environment-protective, product and solvent are easily separated and reclaim the method for the preparing benzaldehyde by oxidizing toluene that toluene conversion in the reaction and phenyl aldehyde selectivity are simultaneously higher.
The present invention addresses the above problem the technical scheme that is adopted: used raw material comprises that weight percent is the toluene of 1-59% in the method for this preparing benzaldehyde by oxidizing toluene, weight percent is the Primary Catalysts of 0.005-5%, the oxygen source that contains oxygen molecule is as the peruscabin of solvent; The weight percent of described peruscabin is 40-98%, and the oxygen molecule in the described oxygen source and the mol ratio of toluene are (0.3-3): 1, and described Primary Catalysts is one or more in cobalt ion, mn ion, vanadium ion, the nickel ion; Toluene, Primary Catalysts and peruscabin be added to obtain mixed solution in the reactor, it is 140-300 ℃ in temperature then, absolute pressure is under the condition of 0.05-1.0Mpa, feeding the oxygen source that contains oxygen molecule in above-mentioned mixed solution reacts, reaction times makes phenyl aldehyde at last more than 2 hours to making with extra care through reacted mixed solution; The transformation efficiency of described toluene is more than 30%, and the selectivity of described phenyl aldehyde is more than 70%.
Comprise in the raw material of the present invention that weight percent is the peruscabin of 75-94%.
Raw material of the present invention comprises that also weight percent is the promotor of 0.005-5%, and this promotor is one or more in cupric ion, iron ion, zine ion, the chromium ion.
Raw material of the present invention also comprises the bromide as promotor.
Primary Catalysts of the present invention is one or more in cobaltous benzoate, manganese benzoate, phenylformic acid vanadium, the nickel benzoate.
The temperature of mixed solution of the present invention when reaction is 180-250 ℃, and absolute pressure is 0.08-0.4Mpa.
The oxygen source that contains oxygen molecule of the present invention is an air.
The present invention compared with prior art has the following advantages and effect: reaction efficiency height, the transformation efficiency of toluene are up to more than 30%, and the selectivity of phenyl aldehyde reaches more than 70%, and the transformation efficiency of toluene and the selectivity of phenyl aldehyde are improved simultaneously greatly; Reaction process is simple, and product and solvent are easily separated, and solvent reclaims easily and utilizes, thereby has reduced production cost and simplified technical process; The waste liquid and the waste residue that are produced in the reaction process are few, and clean environment firendly can not produce environment and destroy.
Adopt peruscabin as solvent, peruscabin is that toluene oxidation prepares one of benzoic by product, generate by esterification by toluene oxidation intermediate product phenylcarbinol and phenylformic acid, therefore, the present invention adopts peruscabin can avoid producing new by product as solvent in reaction system, be convenient to product separation and purification, improve the quality of product.
Primary Catalysts metal ion among the present invention is one or more in cobalt ion, mn ion, vanadium ion, the nickel ion, also can select for use metal ions such as cupric ion, iron ion, zine ion, chromium ion as promotor.The salt of these several metal ion species can be various organic salts and inorganic salt, for avoiding producing other by products, provides the preferred benzoate of salt of metal ion.Because bromine can produce comparatively serious corrosion to stainless steel equipment, under the situation that conversion unit allows, can also select for use bromide as promotor.
The present invention can be that intermittent type carries out, and also can be that continous way is carried out, preferred continuous processing on industrial production.If adopt intermittent type to carry out, the present invention can carry out as follows: add solvent benzol benzyl formate, toluene and catalyzer in reactor, bubbling air keeps having certain pressure in the reactor, unlikely boiling when making reaction solution be heated to temperature of reaction is opened heating then reaction solution is heated to temperature of reaction, by the reaction of certain flow bubbling air, water and methylbenzene azeotropic that reaction generates come out, through condensation and oily water separation, toluene turns back in the reactor, and water is as liquid waste disposal.Stopped reaction when reaction reaches processing requirement is closed air.After going out toluene, phenyl aldehyde, phenylcarbinol and phenylformic acid by fractionation by distillation, contain capable of circulation the applying mechanically of mother liquor of peruscabin and catalyzer, unreacted toluene turns back to and continues reaction in the reactor.Toluene per pass conversion when the present invention adopts intermittent type to carry out reaches more than 30%, and the phenyl aldehyde selectivity reaches more than 70%.
The present invention is if adopt continous way to carry out, the toluene feed mode can adopt the vapor phase toluene charging, the peruscabin that liquid toluene feed or employing are reclaimed, these three kinds of modes of catalyzer and toluene parallel feeding, the preferred peruscabin that reclaims, the mode of catalyzer and toluene parallel feeding, can be with the certain amount of solvent peruscabin, toluene and catalyzer join in the reactor, be heated to temperature of reaction, feed the air of certain flow, add peruscabin with certain flow, the mixed solution of catalyzer and toluene, and constantly emit reaction solution and make the liquid level in the reactor remain on certain height, the reaction solution fractionation by distillation of emitting phenyl aldehyde, phenylcarbinol and phenylformic acid, the purified back of remaining peruscabin and catalyzer mother liquor is mixed with raw material toluene and is turned back in the reactor.Contain toluene, phenyl aldehyde and water in the gas phase on the reactor, fractionation by distillation after condensation, phenyl aldehyde is as product, and peruscabin, catalyzer mother liquor mix with raw material toluene and turn back to continuation reaction in the reactor, and water is as liquid waste disposal.Toluene per pass conversion when the present invention adopts continous way to carry out reaches more than 30%, and the phenyl aldehyde selectivity reaches more than 75%.
Embodiment
The present invention is described in further detail below by embodiment, and following examples are explanation of the invention and the present invention is not limited to following examples.
Embodiment 1:
The method of preparing benzaldehyde by oxidizing toluene is as follows in the present embodiment, in the 500ml reactor, add solvent benzol benzyl formate 240g, toluene 60g and catalyzer cobaltous benzoate 3.0g, open and stir, it is 0.3MPa that bubbling air makes the absolute pressure in the reactor, open heating then reaction solution is heated to 180-185 ℃, the bubbling air flow is 0.4L/min, keeping the absolute pressure of reactor is 0.35MPa, water and methylbenzene azeotropic that reaction generates come out, through condensation and oily water separation, the toluene Returning reactor, water is as liquid waste disposal.Reacted 6 hours, and closed air cooling.Through chromatogram ration analysis, contain toluene 28.6g, phenyl aldehyde 28.3g, phenylcarbinol 3.2g and phenylformic acid 4.2g in the reaction solution, the transformation efficiency of toluene is 52.3%, the selectivity of phenyl aldehyde is 78.3%.After reaction solution goes out toluene, phenyl aldehyde, phenylcarbinol and phenylformic acid by fractionation by distillation, contain capable of circulation the applying mechanically of mother liquor of peruscabin and catalyzer, unreacted toluene reclaims the back and continues reaction next time.
Embodiment 2
With 280g solvent benzol benzyl formate, 20g toluene and 3.0g cobaltous benzoate, 1.0g manganese benzoate joins in the 500ml reactor, open and stir, normal pressure is reaction down, the bubbling air flow is 0.2L/min, being heated to temperature of reaction is 225-230 ℃, flow with 30g/h adds peruscabin, the mixed solution of catalyzer and toluene, content of toluene is 30% in the mixed solution, constantly emitting reaction solution makes the liquid level in the reactor remain on starting altitude, the reaction solution fractionation by distillation of emitting phenyl aldehyde, phenylcarbinol and phenylformic acid add after remaining peruscabin and catalyzer mother liquor are purified that 30% raw material toluene mixes again and turn back in the reactor with the flow velocity of 30g/h; Stop to add the mixed solution of fresh peruscabin, catalyzer and toluene simultaneously.Gas phase on the reaction solution contains toluene, phenyl aldehyde and water, the toluene of gas phase, phenyl aldehyde and water take out of by gas and after condensation fractionation by distillation, phenyl aldehyde is as product, toluene reclaims the back to be continued as raw material, water is as liquid waste disposal.Successive reaction 32 hours is carried out chromatogram ration analysis to reaction solution and all products, gets phenyl aldehyde 257g, phenylformic acid 25g, unreacted toluene 45.8g; The per pass conversion of toluene is 37.3%, and the selectivity of phenyl aldehyde is 85%, and the phenylformic acid selectivity is 7.2%.
Embodiment 3
With 500g solvent benzol benzyl formate, 40g toluene and 6.0g cobaltous benzoate, 1.0g manganese benzoate, 0.5g nickel benzoate joins in the 800ml bubbling column reactor, normal pressure is reaction down, the bubbling air flow is 0.2L/min, being heated to temperature of reaction is 220-225 ℃, flow velocity with 30g/h adds peruscabin, the mixed solution of catalyzer and toluene, toluene level is 30% in the mixed solution, constantly emitting reaction solution makes the interior liquid level of reactor remain on starting altitude, the reaction solution fractionation by distillation of emitting phenyl aldehyde, phenylcarbinol and phenylformic acid, the raw material toluene of remaining peruscabin and the purified adding 30% of catalyzer mother liquor mix and turn back in the reactor with the flow velocity of 30g/h; Stop to add the mixed solution of fresh peruscabin, catalyzer and toluene simultaneously.Contain toluene, phenyl aldehyde and water in the gas phase on the reaction solution, the gas phase that contains toluene, phenyl aldehyde and water take out of by gas and after condensation fractionation by distillation, phenyl aldehyde is as product, toluene reclaims and continues as raw material, water is as liquid waste disposal.Successive reaction 30 hours is carried out chromatogram ration analysis to reaction solution and all products, gets phenyl aldehyde 246g, phenylformic acid 22g, unreacted toluene 65.1g; The toluene per pass conversion is 31.2%, and the phenyl aldehyde selectivity is 87.3%, and the phenylformic acid selectivity is 6.8%.
Embodiment 4
280g solvent benzol benzyl formate, 20g toluene and 3.0g cobaltous benzoate, 1.0g manganese benzoate are joined the 500ml reactor, open and stir, normal pressure is reaction down, and the bubbling air flow is 0.2L/min, and being heated to temperature of reaction is 225-230 ℃, flow with 9g/h adds toluene, gas phase contains toluene, phenyl aldehyde and water on the reaction solution, takes fractionation by distillation after condensation out of by gas, and phenyl aldehyde is as product, toluene reclaims and continues as raw material reaction, and water is as liquid waste disposal.Successive reaction 35 hours is carried out chromatogram ration analysis to reaction solution and all products, gets phenyl aldehyde 229g, phenylformic acid 37.8g, unreacted toluene 83g; The toluene per pass conversion is 30.2%, and the phenyl aldehyde selectivity is 78.7%, and the phenylformic acid selectivity is 11.3%.Reaction solution continues to use after distillation is reclaimed phenyl aldehyde, phenylcarbinol and phenylformic acid and removed other impurity of part.
Embodiment 5
In the 500ml reactor, add solvent benzol benzyl formate 200g, toluene 100g and catalyzer cobaltous benzoate 3.0g, open and stir, it is 0.5MPa that bubbling air makes the interior absolute pressure of reactor, open heating then reaction solution is heated to 180-185 ℃, the bubbling air flow is 0.4L/min, and keeping the reactor absolute pressure is 0.5MPa, water and methylbenzene azeotropic that reaction generates come out, through condensation and oily water separation, toluene turns back in the reactor, and water is as liquid waste disposal.Reacted 7 hours, and closed air cooling.Through chromatogram ration analysis, contain toluene 39.5g in the reaction solution, contain phenyl aldehyde 49.4g, phenylcarbinol 3.9g, phenylformic acid 17.9g, the transformation efficiency of toluene are 60.5%, the phenyl aldehyde selectivity is 70.9%.After reaction solution goes out toluene, phenyl aldehyde, phenylcarbinol and phenylformic acid by fractionation by distillation, contain capable of circulation the applying mechanically of mother liquor of peruscabin and catalyzer, unreacted toluene reclaims and continues secondary response down.
Table 1 embodiment 6-embodiment 11
Table 2 embodiment 12-embodiment 16
| Parameter type | Embodiment 12 | Embodiment 13 | Embodiment 14 | Embodiment 15 | Embodiment 16 |
| Toluene (weight %) | ??17 | ??18 | ??19.5 | ??19.5 | ??20 |
Table 3 embodiment 17-embodiment 21
Table 4 embodiment 22-embodiment 26
The concrete parameter of embodiment 6-embodiment 26 sees Table 1-table 4, and processing method and embodiment 1 among the embodiment 6-embodiment 26 are similar, so locate no longer to describe in detail.Temperature of reaction among the present invention preferably between 180-250 ℃, preferably more than 5 hours, select usually between 5-10 hour by the required reaction times.
Though the present invention with embodiment openly as above; but it is not in order to limit protection scope of the present invention; any technician who is familiar with this technology, change and the retouching done in not breaking away from design of the present invention and scope all should belong to protection scope of the present invention.
Claims (7)
1. the method for a preparing benzaldehyde by oxidizing toluene, used raw material comprises that weight percent is the toluene of 1-59% in this method, weight percent is the Primary Catalysts of 0.005-5%, contains the oxygen source of oxygen molecule, as the peruscabin of solvent; The weight percent of described peruscabin is 40-98%, and the oxygen molecule in the described oxygen source and the mol ratio of toluene are (0.3-3): 1, and described Primary Catalysts is one or more in cobalt ion, mn ion, vanadium ion, the nickel ion; Toluene, Primary Catalysts and peruscabin be added to obtain mixed solution in the reactor, it is 140-300 ℃ in temperature then, absolute pressure is under the condition of 0.05-1.0Mpa, feeding the oxygen source that contains oxygen molecule in above-mentioned mixed solution reacts, reaction times makes phenyl aldehyde at last more than 2 hours to making with extra care through reacted mixed solution; The transformation efficiency of described toluene is more than 30%, and the selectivity of described phenyl aldehyde is more than 70%.
2. the method for preparing benzaldehyde by oxidizing toluene according to claim 1 is characterized in that: comprise in the described raw material that weight percent is the peruscabin of 75-94%.
3. the method for preparing benzaldehyde by oxidizing toluene according to claim 1 and 2, it is characterized in that: described raw material comprises that also weight percent is the promotor of 0.005-5%, and this promotor is one or more in cupric ion, iron ion, zine ion, the chromium ion.
4. the method for preparing benzaldehyde by oxidizing toluene according to claim 1 and 2, it is characterized in that: described raw material also comprises the bromide as promotor.
5. the method for preparing benzaldehyde by oxidizing toluene according to claim 1 and 2, it is characterized in that: described Primary Catalysts is one or more in cobaltous benzoate, manganese benzoate, phenylformic acid vanadium, the nickel benzoate.
6. the method for preparing benzaldehyde by oxidizing toluene according to claim 1 and 2 is characterized in that: the temperature of described mixed solution when reaction is 180-250 ℃, and absolute pressure is 0.08-0.4Mpa.
7. the method for preparing benzaldehyde by oxidizing toluene according to claim 1 and 2, it is characterized in that: the described oxygen source that contains oxygen molecule is an air.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103265416A (en) * | 2013-05-23 | 2013-08-28 | 南京大学 | Method for preparing benzaldehyde from methylbenzene with high selectivity |
| CN104693002A (en) * | 2015-03-11 | 2015-06-10 | 南京工业大学 | Method for preparing benzaldehyde by toluene oxidation |
| CN106883116A (en) * | 2015-12-15 | 2017-06-23 | 中国科学院大连化学物理研究所 | A kind of toluene catalytic oxidation benzoic acid, benzaldehyde, the method for Ergol |
| CN108435188A (en) * | 2015-07-31 | 2018-08-24 | 永春新盛环保科技有限公司 | A kind of preparation method of toluene direct oxidation producing benzaldehyde catalyst |
| CN110075882A (en) * | 2019-05-09 | 2019-08-02 | 南京工程学院 | A kind of application of transition metal composite oxide catalytic agent in catalysis toluene oxidation synthesizing benzoic acids benzyl ester |
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| CN1296937A (en) * | 2000-05-08 | 2001-05-30 | 湖南大学 | Process for preparing benzoic acid, henzaldehyde and benzyl alcohol |
| CN1663941A (en) * | 2004-03-01 | 2005-09-07 | 中国科学院大连化学物理研究所 | Process for synthesizing benzaldehyde by selective oxidation of toluene |
| CN101613269A (en) * | 2008-06-25 | 2009-12-30 | 中国科学院大连化学物理研究所 | A kind of method of preparing phenylformic acid through liquid phase oxidation of methylbenzene |
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2010
- 2010-03-18 CN CN 201010127212 patent/CN101786947B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1296937A (en) * | 2000-05-08 | 2001-05-30 | 湖南大学 | Process for preparing benzoic acid, henzaldehyde and benzyl alcohol |
| CN1663941A (en) * | 2004-03-01 | 2005-09-07 | 中国科学院大连化学物理研究所 | Process for synthesizing benzaldehyde by selective oxidation of toluene |
| CN101613269A (en) * | 2008-06-25 | 2009-12-30 | 中国科学院大连化学物理研究所 | A kind of method of preparing phenylformic acid through liquid phase oxidation of methylbenzene |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103265416A (en) * | 2013-05-23 | 2013-08-28 | 南京大学 | Method for preparing benzaldehyde from methylbenzene with high selectivity |
| CN104693002A (en) * | 2015-03-11 | 2015-06-10 | 南京工业大学 | Method for preparing benzaldehyde by toluene oxidation |
| CN108435188A (en) * | 2015-07-31 | 2018-08-24 | 永春新盛环保科技有限公司 | A kind of preparation method of toluene direct oxidation producing benzaldehyde catalyst |
| CN106883116A (en) * | 2015-12-15 | 2017-06-23 | 中国科学院大连化学物理研究所 | A kind of toluene catalytic oxidation benzoic acid, benzaldehyde, the method for Ergol |
| CN110075882A (en) * | 2019-05-09 | 2019-08-02 | 南京工程学院 | A kind of application of transition metal composite oxide catalytic agent in catalysis toluene oxidation synthesizing benzoic acids benzyl ester |
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