CN102391067A - Method for synthesizing isopropyl alcohol by hydrogenating acetone - Google Patents
Method for synthesizing isopropyl alcohol by hydrogenating acetone Download PDFInfo
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- CN102391067A CN102391067A CN2011102091590A CN201110209159A CN102391067A CN 102391067 A CN102391067 A CN 102391067A CN 2011102091590 A CN2011102091590 A CN 2011102091590A CN 201110209159 A CN201110209159 A CN 201110209159A CN 102391067 A CN102391067 A CN 102391067A
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Abstract
The invention relates to a method for synthesizing isopropyl alcohol by hydrogenating acetone. A catalyst is a nickel oxide catalyst loaded on an alumina carrier, wherein the mass ratio of alumina to nickel oxide is 3:4. The catalyst is black spherical particles of which the specifications are 3-5 millimeters, the bulk density is 0.80-0.85 g/ml, and the strength is 80-120 N/P. The catalyst is reduced in the hydrogen atmosphere at the temperature 200-280 DEG C for 12-48 hours before use. The method comprises the following steps of: gasifying an acetone-hydrogen mixture, and overheating; and feeding into a hydrogenation reactor for undergoing a hydrogenation reaction, wherein the gasifying temperature is 60-100 DEG C, the overheating temperature is 80-120 DEG C, the hydrogenation reaction temperature is 100-160 DEG C, the reaction pressure is 0.6-0.98 MPa, the liquid phase volume space velocity of acetone is 0.1-0.3 h<-1>, and the molar ratio of hydrogen to acetone is 10:20. The method has the advantages of high catalyst selectivity, high strength, low hydrogenation reaction pressure, mild reaction condition, easiness for removing reaction heat, and the like.
Description
Technical field:
The present invention relates to a kind of method of petrohol, particularly a kind of is raw material with acetone, through the method for vapour phase hydrogenation process petrohol.
Background technology:
Virahol (Isopropyl Alcohol is called for short IPA) has another name called secondary propyl alcohol, dimethylcarbinol, is a kind of organic solvent of excellent property, is widely used as the solvent of shellac, Nitrocellulose, vegeto-alkali, rubber and grease etc.Virahol is still produced the important intermediate of multiple organic cpds, can be used as the raw material of synthetic glycerine, isopropyl acetate and acetone etc., also is widely used as oil-fired antifreeze additive, is used for aspects such as automobile and aviation fuel.In addition; Virahol also can be used for making sterilant, sterilant, sanitising agent and disinfection preservative etc.; It can use separately, also can with other alcohol, tensio-active agent and usefulness, have purposes widely in fields such as agricultural chemicals, electronic industry, medicine, coating, daily-use chemical industry and organic syntheses.
The conventional production methods of Virahol mainly is the propylene hydration method in the industry, and its operational path can be divided into two kinds of indirect hydration method and direct hydration methods.Because state's inner propene resource is nervous, the production cost of propylene hydration method petrohol is high.Domestic acetone production capacity is bigger, and dimensions of market is plentiful, and price is lower.The production cost of acetone hydride process petrohol is well below the propylene hydration method.
CN 0012023 discloses a kind of method for hydrogenation of acetone, comprises that at least two method stepss carry out the liquid phase hydrogenation of acetone.Use the nickel-containing catalyst on the alpha-alumina supports, 60-140 ℃ with the 20-50 bar pressure under, water-content is lower than under the condition of 1.0% weight and carries out liquid phase hydrogenation.
CN 02822727 discloses a kind of method for hydrogenation of acetone, and said hydrogenation adopts the nickel catalyzator in the tripoli, accomplishes a kind of being in the multi-tubular reactor that the drip mode operates.
US 7,041, and the liquid phase process that the hydrogenation of 857 pairs of acetone prepares Virahol improves.The promoted sponge metal catalyst of the chromium of empoly effective amount makes acetone contact with hydrogen under the liquid-phase condition continuously.
US 7,799, and 958 disclose a kind of method for preparing Virahol through liquid-phase hydrogenatin.Through at least two hydrogenation reaction stages, be Virahol with acetone liquid-phase hydrogenatin.
CN 200910087777 discloses a kind of nickel-base catalyst and application thereof of preparing isopropyl alcohol by acetone hydrogenation.In nickel-base catalyst, add a spot of Mo and Zn, produce the yield of Virahol with the acetone hydrogenation that improves catalyzer.
CN 200880107503 discloses a kind of method of manufacture and s.t. Reni catalyst of alcohol.Used catalyzer is for contacting the s.t. Reni catalyst that obtains through Reni catalyst with acid
CN 200610154968 discloses a kind of compound method of Virahol.With acetone is raw material, with the Ni-Co/AC catalyzer, and at normal pressure～2.0Mpa, 70～200 ℃ of temperature, ketone liquid phase air speed 1.0～10.0h
-1, hydrogen ketone carries out the vapour phase hydrogenation reaction than 3～15 times.
CN 98121050 discloses a kind of process method by the acetone hydrogenation preparing isopropanol.Adopt the CuO-ZnO oxide mixture catalyst of compression molding, in fixed-bed reactor, preparing isopropyl alcohol by acetone hydrogenation.Wherein the CuO mass percent is 25～75%, and the ZnO mass percent is 20～70%.
CN02822695 discloses a kind of preparation method of Virahol.The acetone raw material hydrogenation that use is polluted by benzene obtains the hydrogenation products of Virahol and benzene.
CN200980101713 discloses a kind of method of manufacture of 2-propyl alcohol, in the presence of hydrogenation catalyst, makes the raw material and the hydrogen that contain water and acetone react petrohol.Preferred hydrogenation catalyst is Raney's nickel and CuO～ZnO catalyst.
Acetone liquid phase hydrogenation petrohol reaction pressure is high, and facility investment is big.And the heat exchange efficiency of vapour phase hydrogenation petrohol reaction is low usually, and heat of reaction can't shift out when industrial production, poor operability.
Summary of the invention:
The object of the present invention is to provide a kind of reaction conditions gentle, be fit to the method for industrial acetone vapour phase hydrogenation petrohol.
Technical scheme of the present invention can realize like this:
In reactor drum, load hydrogenation catalyst, catalyzer is a kind of nickel oxide catalyst that loads on the alumina supporter, wherein aluminum oxide: the nickel oxide mass ratio is 3～4.The catalyzer outward appearance is the black spherical particle, and specification is 3～5mm, and bulk density is 0.80～0.85g/ml, and intensity is 80～120N/P.Catalyzer reduced 12～48 hours in 200～280 ℃ of hydrogen atmospheres before using.After acetone and the gasification of hydrogen mixture process are overheated, get into hydrogenation takes place in the hydrogenation reactor.Gasification temperature is 60～100 ℃, and temperature of superheat is 80-120 ℃.The hydrogenation temperature is 100～160 ℃, reaction pressure 0.6～0.98MPa, and acetone solution phase volume air speed is 0.1-0.3h
-1, hydrogen and acetone mol ratio are 10～20.
The method of a kind of petrohol provided by the invention compared with prior art has following advantage:
1, hydrogenation reaction pressure is low, and reaction conditions is gentle, and facility investment is few.
2, catalyst selectivity is high, and intensity is good, can use than under the condition at high hydrogen ketone.
3, heat of reaction can shift out from reactor drum fast, helps the stable control of temperature of reaction.
Embodiment:
Combine embodiment at present, the present invention described in detail as follows:
Embodiment 1
Get 3 parts of 3～5mm ball-aluminium oxides by weight, 1 part of Nickelous nitrate hexahydrate in nickel oxide adopts equi-volume impregnating to prepare nickel oxide-aluminium oxide catalyst.Behind room temperature dipping 4h, through 120 ℃ of oven dry, 450 ℃ of roastings obtain aluminum oxide: the nickelous nitrate mass ratio is 3 catalyzer CA-1.Recording catalyst bulk density is 0.85g/ml, and catalyst strength is 79N/P.
Embodiment 2
Get 3.5 parts of 3～5mm ball-aluminium oxides by weight, 1 part of Nickelous nitrate hexahydrate in nickel oxide adopts equi-volume impregnating to prepare nickel oxide-aluminium oxide catalyst.Behind room temperature dipping 4h, through 120 ℃ of oven dry, 450 ℃ of roastings obtain aluminum oxide: the nickelous nitrate mass ratio is 3 catalyzer CA-2.Recording catalyst bulk density is 0.84g/ml, and catalyst strength is 96N/P.
Embodiment 3
Get 4 parts of 3～5mm ball-aluminium oxides by weight, 1 part of Nickelous nitrate hexahydrate in nickel oxide adopts equi-volume impregnating to prepare nickel oxide-aluminium oxide catalyst.Behind room temperature dipping 4h, through 120 ℃ of oven dry, 450 ℃ of roastings obtain aluminum oxide: the nickelous nitrate mass ratio is 3 catalyzer CA-3.Recording catalyst bulk density is 0.80g/ml, and catalyst strength is 122N/P.
Embodiment 4
Catalyzer CA-1 is pulverized, get granularity product 100ml between the 10-20 order, in the fixed-bed reactor of packing into.With the nitrogen replacement system qualified after, heat up with the speed of 50 ℃/h, when temperature reaches 200 ℃; Slowly feed hydrogen, the control catalyst bed temperature is no more than 300 ℃, after reaction bed temperature is stable; Improve reduction temperature to 280 ℃; Speed with 0.2l/min feeds hydrogen, and constant temperature was cooled to 100 ℃ after 12 hours.After acetone and the gasification of hydrogen mixture process are overheated, get into hydrogenation takes place in the hydrogenation reactor.Gasification temperature is 60 ℃, and temperature of superheat is 80 ℃.In temperature of reaction is 100 ℃, reaction pressure 0.8MPa, and acetone solution phase volume air speed is 0.1h
-1, hydrogen and acetone mol ratio are to carry out hydrogenation under 10 conditions, the gc analysis crude product is formed.Acetone conversion is 99.52%, the Virahol selectivity is 99.92%.
Embodiment 5
Catalyzer CA-1 is pulverized, get granularity product 100ml between the 10-20 order, in the fixed-bed reactor of packing into.With the nitrogen replacement system qualified after, heat up with the speed of 50 ℃/h, when temperature reaches 200 ℃; Slowly feed hydrogen, the control catalyst bed temperature is no more than 300 ℃, after reaction bed temperature is stable; Improve reduction temperature to 280 ℃; Speed with 0.2l/min feeds hydrogen, and constant temperature was cooled to 100 ℃ after 48 hours.After acetone and the gasification of hydrogen mixture process are overheated, get into hydrogenation takes place in the hydrogenation reactor.Gasification temperature is 80 ℃, and temperature of superheat is 120 ℃.In temperature of reaction is 160 ℃, reaction pressure 0.98MPa, and acetone solution phase volume air speed is 0.3h
-1, hydrogen and acetone mol ratio are to carry out hydrogenation under 20 conditions, the gc analysis crude product is formed.Acetone conversion is 99.71%, the Virahol selectivity is 99.41%.
Embodiment 6
Catalyzer CA-2 is pulverized, get granularity product 100ml between the 10-20 order, in the fixed-bed reactor of packing into.With the nitrogen replacement system qualified after, heat up with the speed of 50 ℃/h, when temperature reaches 200 ℃; Slowly feed hydrogen, the control catalyst bed temperature is no more than 300 ℃, after reaction bed temperature is stable; Improve reduction temperature to 280 ℃; Speed with 0.2l/min feeds hydrogen, and constant temperature was cooled to 100 ℃ after 24 hours.After acetone and the gasification of hydrogen mixture process are overheated, get into hydrogenation takes place in the hydrogenation reactor.Gasification temperature is 100 ℃, and temperature of superheat is 120 ℃.In temperature of reaction is 140 ℃, reaction pressure 0.9MPa, and acetone solution phase volume air speed is 0.2h
-1, hydrogen and acetone mol ratio are to carry out hydrogenation under 18 conditions, the gc analysis crude product is formed.Acetone conversion is 99.19%, the Virahol selectivity is 99.87%.
Embodiment 7
Catalyzer CA-2 is pulverized, get granularity product 100ml between the 10-20 order, in the fixed-bed reactor of packing into.With the nitrogen replacement system qualified after, heat up with the speed of 50 ℃/h, when temperature reaches 200 ℃; Slowly feed hydrogen, the control catalyst bed temperature is no more than 300 ℃, after reaction bed temperature is stable; Improve reduction temperature to 280 ℃; Speed with 0.2l/min feeds hydrogen, and constant temperature was cooled to 100 ℃ after 24 hours.After acetone and the gasification of hydrogen mixture process are overheated, get into hydrogenation takes place in the hydrogenation reactor.Gasification temperature is 100 ℃, and temperature of superheat is 120 ℃.In temperature of reaction is 150 ℃, reaction pressure 0.9MPa, and acetone solution phase volume air speed is 0.2h
-1, hydrogen and acetone mol ratio are to carry out hydrogenation under 10 conditions, the gc analysis crude product is formed.Acetone conversion is 99.36%, the Virahol selectivity is 99.85%.
Embodiment 8
Catalyzer CA-3 is pulverized, get granularity product 100ml between the 10-20 order, in the fixed-bed reactor of packing into.With the nitrogen replacement system qualified after, heat up with the speed of 50 ℃/h, when temperature reaches 200 ℃; Slowly feed hydrogen, the control catalyst bed temperature is no more than 300 ℃, after reaction bed temperature is stable; Improve reduction temperature to 280 ℃; Speed with 0.2l/min feeds hydrogen, and constant temperature was cooled to 100 ℃ after 24 hours.After acetone and the gasification of hydrogen mixture process are overheated, get into hydrogenation takes place in the hydrogenation reactor.Gasification temperature is 80 ℃, and temperature of superheat is 90 ℃.In temperature of reaction is 145 ℃, reaction pressure 0.8MPa, and acetone solution phase volume air speed is 0.1h
-1, hydrogen and acetone mol ratio are to carry out hydrogenation under 18 conditions, the gc analysis crude product is formed.Acetone conversion is 99.73%, the Virahol selectivity is 99.49%
Embodiment 9
Catalyzer CA-3 is pulverized, get granularity product 100ml between the 10-20 order, in the fixed-bed reactor of packing into.With the nitrogen replacement system qualified after, heat up with the speed of 50 ℃/h, when temperature reaches 200 ℃; Slowly feed hydrogen, the control catalyst bed temperature is no more than 300 ℃, after reaction bed temperature is stable; Improve reduction temperature to 280 ℃; Speed with 0.2l/min feeds hydrogen, and constant temperature was cooled to 100 ℃ after 24 hours.After acetone and the gasification of hydrogen mixture process are overheated, get into hydrogenation takes place in the hydrogenation reactor.Gasification temperature is 80 ℃, and temperature of superheat is 90 ℃.In temperature of reaction is 145 ℃, reaction pressure 0.8MPa, and acetone solution phase volume air speed is 0.3h
-1, hydrogen and acetone mol ratio are to carry out hydrogenation under 18 conditions, the gc analysis crude product is formed.Acetone conversion is 99.36%, the Virahol selectivity is 99.55%.
Claims (5)
1. the method for an acetone hydrogenation petrohol, it is characterized in that adopting a kind of nickel oxide catalyst that loads on the alumina supporter, wherein aluminum oxide: the nickel oxide quality is 3～4 than content.
2. catalyzer according to claim 1 is characterized in that catalyzer is the black spherical particle, and specification is 3～5mm, and bulk density is 0.80～0.85g/ml, and intensity is 80～120N/P.
3. catalyzer according to claim 1 is characterized in that in 200～280 ℃ of hydrogen atmospheres, reducing 12～48 hours before catalyzer uses.
4. according to the method for the said petrohol of claim 1; After it is characterized in that the gasification of acetone and hydrogen mixture process is overheated, get into hydrogenation takes place in the hydrogenation reactor, temperature of reaction is 100～160 ℃; Reaction pressure 0.6～0.98MPa, acetone solution phase volume air speed is 0.1-0.3h
-1, hydrogen and acetone mol ratio are 10～20.
5. according to the method for the said petrohol of claim 4, the gasification temperature that it is characterized in that acetone and hydrogen mixture is 60～100 ℃, and temperature of superheat is 80-120 ℃.
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| CN2011102091590A CN102391067A (en) | 2011-07-21 | 2011-07-21 | Method for synthesizing isopropyl alcohol by hydrogenating acetone |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108654618A (en) * | 2017-03-28 | 2018-10-16 | 锦湖石油化学株式会社 | Metal oxide catalyst, preparation method and the preparation method using its alcohol |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4258268A (en) * | 1979-08-27 | 1981-03-24 | Phillips Petroleum Company | Polycyclic phenols, alcohols and ketones from phenols, cyclic alcohols and cyclic ketones using a nickel oxide/manganese oxide/magnesium oxide catalyst in presence of at least one of hydrogen and nitrogen |
| JPH03141235A (en) * | 1989-10-24 | 1991-06-17 | Mitsui Petrochem Ind Ltd | Production of isopropanol |
| CN1927794A (en) * | 2005-09-07 | 2007-03-14 | 气体产品与化学公司 | Hydrogenation of acetone |
| CN101815695A (en) * | 2007-10-04 | 2010-08-25 | 英尼奥斯石炭酸两合公司 | Process for the production of iso-propanol by liquid phase hydrogenation |
| CN101890351A (en) * | 2009-05-21 | 2010-11-24 | 中国石油化工股份有限公司 | Eggshell type nickel-based catalyst |
| CN101927168A (en) * | 2009-06-26 | 2010-12-29 | 中国石油化工股份有限公司 | Nickel-based catalyst for preparing isopropyl alcohol by acetone hydrogenation and application thereof |
| CN102728361A (en) * | 2011-04-02 | 2012-10-17 | 中国石油化工股份有限公司 | Catalyst for isopropyl alcohol preparation through acetone hydrogenation and application thereof |
-
2011
- 2011-07-21 CN CN2011102091590A patent/CN102391067A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4258268A (en) * | 1979-08-27 | 1981-03-24 | Phillips Petroleum Company | Polycyclic phenols, alcohols and ketones from phenols, cyclic alcohols and cyclic ketones using a nickel oxide/manganese oxide/magnesium oxide catalyst in presence of at least one of hydrogen and nitrogen |
| JPH03141235A (en) * | 1989-10-24 | 1991-06-17 | Mitsui Petrochem Ind Ltd | Production of isopropanol |
| CN1927794A (en) * | 2005-09-07 | 2007-03-14 | 气体产品与化学公司 | Hydrogenation of acetone |
| CN101815695A (en) * | 2007-10-04 | 2010-08-25 | 英尼奥斯石炭酸两合公司 | Process for the production of iso-propanol by liquid phase hydrogenation |
| CN101890351A (en) * | 2009-05-21 | 2010-11-24 | 中国石油化工股份有限公司 | Eggshell type nickel-based catalyst |
| CN101927168A (en) * | 2009-06-26 | 2010-12-29 | 中国石油化工股份有限公司 | Nickel-based catalyst for preparing isopropyl alcohol by acetone hydrogenation and application thereof |
| CN102728361A (en) * | 2011-04-02 | 2012-10-17 | 中国石油化工股份有限公司 | Catalyst for isopropyl alcohol preparation through acetone hydrogenation and application thereof |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108654618A (en) * | 2017-03-28 | 2018-10-16 | 锦湖石油化学株式会社 | Metal oxide catalyst, preparation method and the preparation method using its alcohol |
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Application publication date: 20120328 |