CN102659514A - Method for producing sec-butyl alcohol - Google Patents
Method for producing sec-butyl alcohol Download PDFInfo
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- CN102659514A CN102659514A CN2012101257343A CN201210125734A CN102659514A CN 102659514 A CN102659514 A CN 102659514A CN 2012101257343 A CN2012101257343 A CN 2012101257343A CN 201210125734 A CN201210125734 A CN 201210125734A CN 102659514 A CN102659514 A CN 102659514A
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Abstract
The invention provides a method for producing sec-butyl alcohol through the catalytic hydrolysis of alcohol sec-butyl acetate. The method comprises the following steps of: carrying out continuously catalytic hydrolysis in a stationary bed by using the alcohol sec-butyl acetate as a raw material, and filling a catalyst in continuous tubes of the cascade multitubular stationary bed, wherein a commercial styrene cation exchange resin catalyst is used as the catalyst, and the cascade multitubular stationary bed comprises multiple identical multitubular reactors; leading the raw material alcohol sec-butyl acetate and water to enter the multitubular reactors, carrying out continuously catalytic hydrolysis reaction under the action of the catalyst to generate a sec-butyl alcohol crude product, and refining the crude product to obtain the sec-butyl alcohol with high purity. The method for producing the sec-butyl alcohol has the advantages that the conversion rate of the sec-butyl alcohol is high, the application range of the alcohol sec-butyl acetate can be increased, and the additional value of the alcohol sec-butyl acetate is increased; and therefore, the method has market promotion value.
Description
Technical field
The present invention relates to a kind of method of producing sec-butyl alcohol, particularly a kind of 2-butyl acetate catalytic hydrolysis is produced the method for sec-butyl alcohol.
Technical background
N-butene is the lower a kind of petrochemical by-product of chemical industry utilization ratio.Before the eighties; Because iso-butylene fails to find the approach of rational Application in the hybrid C 4 component; From the C4 component, separate n-butene exploitation chemical utilization and need special separating unit; Cause cost higher and seem inessential, along with the construction of MTBE production equipment, n-butene (1-butylene and the 2-butylene) concentration that consumes in the C4 component behind the iso-butylene has become very high.Particularly in the 1-butylene separating technology, the purity of by-product 2-butylene can reach 95%, if can the higher fine chemical product of supervene value, will act as a fuel to sell produces bigger benefit.Wherein, utilize one of approach with the n-butene for what the raw material production 2-butyl acetate became n-butene.
The working method of 2-butyl acetate has two kinds at present: pure esterification process and n-butene additive process.The former comprises sec-butyl alcohol and acetic acid esterification and sec-butyl alcohol and anhydride reaction, and the latter is by anhydrous Glacial acetic acid min. 99.5 and n-butene (2-butylene) addition reaction and directly synthetic under an acidic catalyst effect.Because the olefin processes production cost is lower more than 1/3 than pure esterification process, therefore, the alkene additive process is the developing direction of acetic acid synthesized secondary butyl ester.
" the alkene additive process one-step synthesis sec-butyl acetate Technology " of Hunan Zhongchuang Chemical Co., Ltd's exploitation reached the cleaner production standard, meets environmental protection requirement, produces 20,000 tons of sec-butyl acetates, filled up domestic blank.
Because 2-butyl acetate has octane value height, nontoxic, non-corrosiveness; Characteristics such as oxygen level is low are can substitute MTBE to add the new chemical article of component as gasoline, obtain certain application at home; But, country implements along with forbidding the regulation of in gasoline, adding 2-butyl acetate; Domestic 2-butyl acetate production capacity occurs superfluous, and because of the market shrink, supply exceed demand for 2-butyl acetate.Come reducing the inventories so press for the exploitation derived product.
The process method of a CN200810016495 continuously producing sec-butyl alcohol by direct hydration of n-butene, in the presence of the strong acid ion exchange resin catalyzer, fresh n-butene raw material and circulation n-butene are mixed into hydration reactor and carry out hydration reaction; Getting into the crude product separating unit then separates; Set up the n-butene refined unit, by the isolated unreacted n-butene of crude product separating unit, a part is back to hydration reactor as the circulation n-butene and continues to participate in hydration reaction; Another part is sent to the n-butene refined unit and is made with extra care; Remove butane, reclaim n-butene, continue to use as fresh n-butene raw material.
The method of CN97116406 low-carbon alkene direct hydration continuous production low-carbon alcohol, in the presence of the strongly acidic cation-exchange catalyzer, the raw material hydrocarbon that contains low-carbon alkene is with after raw water and recycle hydrocarbons mix; Get into main reactor; Get into the crude product tripping device then, it is characterized in that behind the crude product tripping device, also being provided with auxiliary reactor and phase separator, return main reactor as recycle hydrocarbons by the unreacted hydrocarbon component part that contains low-carbon alkene in main reactor that the crude product tripping device comes out; Another part is with after deionized water mixes; Get in the auxiliary reactor and further carry out hydration reaction, reaction product gets in the phase separator separates isolated aqueous solution of alcohol; Raw water as main reactor gets into main reactor, isolating hydrocarbon phase discharger.
Above patent has following shortcoming for the butylene direct hydration reacts the production route of producing sec-butyl alcohol:
1) per pass conversion is low, less than 10%.
2) high to raw material n-butene concentration requirement, need carry and could use after dense.
3) temperature of reaction is high, and more than 140 ℃, energy consumption is big.
Li Fengyun is in " utilizing heteropolyacid to synthesize sec-butyl alcohol " literary composition; Use heteropolyacid to be catalyzer, anhydrous Glacial acetic acid min. 99.5 and n-butene (2-butylene) addition reaction generates 2-butyl acetate, and the 2-butyl acetate hydrolysis has generated sec-butyl alcohol then; Its hydrolysis is mainly and directly adds water, hydrolysis under acidic conditions.This method makes butylene produce sec-butyl alcohol through indirect method, has widened the application market of 2-butyl acetate.But shortcomings such as this method uses heteropolyacid to have transformation efficiency low as catalyzer, and by product is many, and hydrolysis is not thorough need to solve.
Summary of the invention
To the deficiency of prior art, the method for a kind of new production sec-butyl alcohol of the present invention is the method that a kind of 2-butyl acetate catalytic hydrolysis is produced sec-butyl alcohol, may further comprise the steps:
With the 2-butyl acetate is raw material; Carry out the hydrolysis of fixed bed continuous catalysis, catalyzer adopts commercially available styrene type cation exchange resin catalyzer, is loaded in the calandria type fixed bed successive pipe of series connection; Described series connection is calandria type fixed bed to comprise a plurality of duplicate shell and tube reactors; Raw material 2-butyl acetate and water get into shell and tube reactor, and the continuous catalysis hydrolysis reaction generates the sec-butyl alcohol bullion under catalyst action, again through making the high purity sec-butyl alcohol.
Described styrene type cation exchange resin catalyzer is selected from the A35 resin catalyst of U.S.'s ROHM AND HAAS production or the D006 resin catalyst that KaiRui Chemical Engineering Co., Ltd produces.
Described series connection is calandria type fixed bed to be preferably placed in-line 3 duplicate shell and tube reactors.
The water ester mol ratio of described raw material 2-butyl acetate and water is 2～6.
Described continuous catalysis hydrolysis reaction, 80～100 ℃ of preferable reaction temperature, air speed 0.5-8/h, reaction pressure 1～3MPa.
The method that a kind of preferred 2-butyl acetate catalytic hydrolysis of the present invention is produced sec-butyl alcohol, realize through following steps:
1). the 2-butyl acetate catalytic hydrolysis
Hydrolysis reaction adopts the calandria type fixed bed continuous catalysis device of series connection, and this device comprises 3 duplicate reaction towers, connects with series system;
Catalyzer adopts commercially available styrene type cation exchange resin catalyzer, and the expansion space is reserved in the resin catalyst filling, and 2-butyl acetate and water normal temperature mix down; Pass through 3 placed in-line reactor drums successively with the mol ratio of water to ester ratio 2～6, the air speed of 0.5-8/h, hydrolytic reactions generates sec-butyl alcohol, 80～100 ℃ of temperature of reaction under catalyst action; Reaction pressure 1～3MPa; Water coolant carries out heat exchange to 3 reaction towers simultaneously with concurrent, takes away unnecessary heat of reaction, control reaction temperature;
2-butyl acetate directly and water catalysis hydrolytic reactions be the fixed bed catalyst process; Use the heatproof cation exchange resin catalyst in the tubulation; The raw material 2-butyl acetate directly passes through the beds hydrolytic reactions with water with the liquid phase laminar flow regime;, reaction generates sec-butyl alcohol under catalyst action.
2). making with extra care of sec-butyl alcohol
The sec-butyl alcohol that step 1) is obtained and the mixture standing demix of water separate, and obtain highly purified sec-butyl alcohol.
The preparation method of this invention has following beneficial effect:
(1). overcome the reaction of butylene direct hydration and produced the low shortcoming of sec-butyl alcohol transformation efficiency, transformation efficiency is greater than 95%.
(2). open up the new purposes of 2-butyl acetate, solved the product overloading problem.
Embodiment
Following instance only is to further specify the present invention, is not the scope of restriction the present invention protection.
Embodiment 1:
Main raw material
2-butyl acetate, Hunan Zhongchuang Chemical Co., Ltd, carbon four is produced with the acetic acid additive process behind the ether.
Deionized water, self-control.
The D006 resin catalyst, KaiRui Chemical Engineering Co., Ltd.
1). the 2-butyl acetate catalytic hydrolysis
The calandria type fixed bed continuous catalysis testing apparatus of series connection that experiment is adopted.This system comprises 3 duplicate reaction towers, connects with series system, and reaction tower diameter Di=240mm, pipe adopts 316 stainless steels, conduit outside diameter d 0=8mm, effective tube length L=3m, pipe radical n=15 root, rounded projections arranged.
The D006 resin catalyst that catalyzer adopts KaiRui Chemical Engineering Co., Ltd to produce.The resin catalyst packing factor is controlled at 70%, reserves the expansion space.Mix after the reaction mass preheating, with the mol ratio of setting, air speed is successively through 3 placed in-line reactor drums, and the water coolant that adopts between pipe adopts concurrent simultaneously 3 reaction towers to be carried out heat exchange, takes away unnecessary heat of reaction control reaction temperature.2-butyl acetate directly and water catalysis hydrolytic reactions be the fixed bed catalyst process; Use the heatproof cation exchange resin catalyst in the tubulation, the raw material 2-butyl acetate directly passes through beds hydrolytic reactions, 100 ℃ of temperature of reaction with water with the liquid phase laminar flow regime; Air speed 0.5/h; Water ester mol ratio 2, reaction pressure 1MPa, reaction generates sec-butyl alcohol under catalyst action.
2). making with extra care of sec-butyl alcohol
Sec-butyl alcohol separates with the water static layering.
The embodiment PIN is KRB-1.
Embodiment 2
The raw material air speed is 8/h, and other is with embodiment 1.Products obtained therefrom is numbered KRB-2.
Embodiment 3
The raw material air speed is 4/h, and other is with embodiment 1.Products obtained therefrom is numbered KRB-3.
Embodiment 4
Water to ester ratio is 6 (mol/mol), and other is with embodiment 1.Products obtained therefrom is numbered KRB-4.
Embodiment 5
Water to ester ratio is 6 (mol/mol), and other is with embodiment 2.Products obtained therefrom is numbered KRB-5.
Embodiment 6
Water to ester ratio is 6 (mol/mol), and other is with embodiment 3.Products obtained therefrom is numbered KRB-6.
Embodiment 7
Water to ester ratio is 4 (mol/mol), and other is with embodiment 1.Products obtained therefrom is numbered KRB-7.
Embodiment 8
Water to ester ratio is 4 (mol/mol), and other is with embodiment 2.Products obtained therefrom is numbered KRB-8.
Embodiment 9
Water to ester ratio is 4 (mol/mol), and other is with embodiment 3.Products obtained therefrom is numbered KRB-9.
Embodiment 10
Reaction pressure is 3MPa, and other is with embodiment 1.Products obtained therefrom is numbered KRB-10.
Embodiment 11
Reaction pressure is 3MPa, and other is with embodiment 2.Products obtained therefrom is numbered KRB-11.
Embodiment 12
Reaction pressure is 3MPa, and other is with embodiment 3.Products obtained therefrom is numbered KRB-12.
Embodiment 13
Reaction pressure is 3MPa, and other is with embodiment 4.Products obtained therefrom is numbered KRB-13.
Embodiment 14
Reaction pressure is 3MPa, and other is with embodiment 5.Products obtained therefrom is numbered KRB-14.
Embodiment 15
Reaction pressure is 3MPa,, other is with embodiment 6.Products obtained therefrom is numbered KRB-15.
Embodiment 16
Reaction pressure is 2MPa, and other is with embodiment 1.Products obtained therefrom is numbered KRB-16.
Embodiment 17
Reaction pressure is 2MPa, and other is with embodiment 2.Products obtained therefrom is numbered KRB-17.
Embodiment 18
Reaction pressure is 2MPa, and other is with embodiment 3.Products obtained therefrom is numbered KRB-18.
Embodiment 19
The conversion zone temperature, 80 ℃, other is with embodiment 1.Products obtained therefrom is numbered KRB-19.
Embodiment 20
The conversion zone temperature, 80 ℃, other is with embodiment 2.Products obtained therefrom is numbered KRB-20.
Embodiment 21
The conversion zone temperature, 80 ℃, other is with embodiment 3.Products obtained therefrom is numbered KRB-21.
Embodiment 22
The conversion zone temperature, 80 ℃, other is with embodiment 4.Products obtained therefrom is numbered KRB-22.
Embodiment 23
The conversion zone temperature, 80 ℃, other is with embodiment 5.Products obtained therefrom is numbered KRB-23.
Embodiment 24
The conversion zone temperature, 80 ℃, other is with embodiment 6.Products obtained therefrom is numbered KRB-24.
Embodiment 25
The conversion zone temperature, 80 ℃, other is with embodiment 7.Products obtained therefrom is numbered KRB-25.
Embodiment 26
The conversion zone temperature, 80 ℃, other is with embodiment 8.Products obtained therefrom is numbered KRB-26.
Embodiment 27
The conversion zone temperature, 80 ℃, other is with embodiment 9.Products obtained therefrom is numbered KRB-27.
Embodiment 28
The conversion zone temperature, 80 ℃, other is with embodiment 10.Products obtained therefrom is numbered KRB-28.
Embodiment 29
The conversion zone temperature, 80 ℃, other is with embodiment 11.Products obtained therefrom is numbered KRB-29.
Embodiment 30
The conversion zone temperature, 80 ℃, other is with embodiment 12.Products obtained therefrom is numbered KRB-30.
Embodiment 31
The conversion zone temperature, 80 ℃, other is with embodiment 13.Products obtained therefrom is numbered KRB-31.
Embodiment 32
The conversion zone temperature, 80 ℃, other is with embodiment 14.Products obtained therefrom is numbered KRB-32.
Embodiment 33
The conversion zone temperature, 80 ℃, other is with embodiment 15.Products obtained therefrom is numbered KRB-33.
Embodiment 34
The conversion zone temperature, 80 ℃, other is with embodiment 16.Products obtained therefrom is numbered KRB-34.
Embodiment 35
The conversion zone temperature, 80 ℃, other is with embodiment 17.Products obtained therefrom is numbered KRB-35.
Embodiment 36
The conversion zone temperature, 80 ℃, other is with embodiment 18.Products obtained therefrom is numbered KRB-36.
Comparative Examples 1:
Use the reaction of butylene direct hydration to produce sec-butyl alcohol
Butylene direct hydration reaction evaluation experiment 10L reactor drum is divided into four sections; The every section filling high temperature of anti-D008 strong acid cation exchange resin catalyst 1L; The n-butene raw material is from passing through four sections beds down; Process water is from four sections entering in bed lower section of every section catalyzer, and reaction generates sec-butyl alcohol under the effect of catalyzer.The SBA that reaction generates flows out from reactor head, and reacted process water flows out from each overflow weir bottom, bed top, through after the water treatment, recycles.150 ℃ of temperature of reaction, butylene air speed 1.7/h, reaction pressure 6.0MPa, water alkene mol ratio 1.1, table 1 is seen in the butene conversion contrast.
The comparison of table 1. different ingredients sample butylene per pass conversion and specific conductivity
| Numbering | Butene conversion % |
| KRB-1 | 99.2 |
| KRB-2 | 99.8 |
| KRB-3 | 99.6 |
| KRB-4 | 97.5 |
| KRB-5 | 99.3 |
| KRB-6 | 98.9 |
| KRB-7 | 99.2 |
| KRB-8 | 98.2 |
| KRB-9 | 98.2 |
| KRB-10 | 99.6 |
| KRB-11 | 99.9 |
| KRB-12 | 99.6 |
| KRB-13 | 98.6 |
| KRB-14 | 99.8 |
| KRB-15 | 99.8 |
| KRB-16 | 96.9 |
| KRB-17 | 99.5 |
| KRB-18 | 99.7 |
| KRB-19 | 93.2 |
| KRB-20 | 91.7 |
| KRB-21 | 90.3 |
| KRB-22 | 90.6 |
| KRB-23 | 91.1 |
| KRB-24 | 90.8 |
| KRB-25 | 92.9 |
| KRB-26 | 91.5 |
| KRB-27 | 93.2 |
| KRB-28 | 91.5 |
| KRB-29 | 92.1 |
| KRB-30 | 91.6 |
| KRB-31 | 91.8 |
| KRB-32 | 90.5 |
| KRB-33 | 90.6 |
| KRB-34 | 92.9 |
| KRB-35 | 90.8 |
| KRB-36 | 90.2 |
| Comparative Examples 1 | 6.5 |
Can know that by last table a kind of 2-butyl acetate of the present invention method that calandria type fixed bed catalytic hydrolysis is produced sec-butyl alcohol of connecting can improve the range of application of 2-butyl acetate, improves the added value of 2-butyl acetate, is a kind of invention with market popularization value.
Claims (6)
1. a 2-butyl acetate catalytic hydrolysis is produced the method for sec-butyl alcohol, may further comprise the steps:
With the 2-butyl acetate is raw material; Carry out the hydrolysis of fixed bed continuous catalysis, catalyzer adopts commercially available styrene type cation exchange resin catalyzer, is loaded in the calandria type fixed bed successive pipe of series connection; Described series connection is calandria type fixed bed to comprise a plurality of duplicate shell and tube reactors; Raw material 2-butyl acetate and water get into shell and tube reactor, and the continuous catalysis hydrolysis reaction generates the sec-butyl alcohol bullion under catalyst action, again through making the high purity sec-butyl alcohol.
2. the described method of claim 1 is characterized in that: described styrene type cation exchange resin catalyzer is selected from the D006 resin catalyst that A35 resin catalyst that U.S.'s ROHM AND HAAS produces or KaiRui Chemical Engineering Co., Ltd produce.
3. the described method of claim 1 is characterized in that: described series connection is calandria type fixed bed to be placed in-line 3 duplicate shell and tube reactors.
4. the described method of claim 1, it is characterized in that: the water ester mol ratio of described raw material 2-butyl acetate and water is 2～6.
5. the described method of claim 1 is characterized in that: described continuous catalysis hydrolysis reaction, 80～100 ℃ of temperature of reaction, air speed 0.5-8/h, reaction pressure 1～3MPa.
6. the described method of claim 1 is characterized in that, realizes through following steps:
1). the 2-butyl acetate catalytic hydrolysis
Hydrolysis reaction adopts the calandria type fixed bed continuous catalysis device of series connection, and this device comprises 3 duplicate reaction towers, connects with series system;
Catalyzer adopts commercially available styrene type cation exchange resin catalyzer, and the expansion space is reserved in the resin catalyst filling, and 2-butyl acetate and water normal temperature mix down; Pass through 3 placed in-line reactor drums successively with the mol ratio of water to ester ratio 2～6, the air speed of 0.5-8/h, hydrolytic reactions generates sec-butyl alcohol, 80～100 ℃ of temperature of reaction under catalyst action; Reaction pressure 1～3MPa; Water coolant carries out heat exchange to 3 reaction towers simultaneously with concurrent, takes away unnecessary heat of reaction, control reaction temperature;
2). making with extra care of sec-butyl alcohol
The sec-butyl alcohol that step 1) is obtained and the mixture of water are put layering silently and are separated, and obtain highly purified sec-butyl alcohol.
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Cited By (13)
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|---|---|---|---|---|
| CN102838450A (en) * | 2012-09-20 | 2012-12-26 | 福州大学 | Method for catalyzing synthesizing sec-butyl alcohol through cation exchange resin |
| CN102964243A (en) * | 2012-11-16 | 2013-03-13 | 北京石油化工学院 | Preparation method of sec-butyl acetate |
| CN104311390A (en) * | 2014-10-17 | 2015-01-28 | 深圳市飞扬实业有限公司 | Method for synthesizing sec-butyl alcohol |
| CN104475109A (en) * | 2014-11-20 | 2015-04-01 | 北京恩泽福莱科技有限公司 | Catalyst for preparing sec-butyl alcohol and preparation method of catalyst |
| CN105130745A (en) * | 2015-07-22 | 2015-12-09 | 深圳市前海飞扬新能源科技有限公司 | Method of producing sec-butyl alcohol |
| CN106554275A (en) * | 2015-09-25 | 2017-04-05 | 中国石油化工股份有限公司 | A kind of method comprehensively utilized by C-4-fraction after ether |
| CN106631684A (en) * | 2015-10-31 | 2017-05-10 | 湖南中创化工股份有限公司 | Method for preparing SBA(sec-butyl alcohol) through hydrolysis with sec-butyl acetate |
| CN106631699A (en) * | 2015-10-31 | 2017-05-10 | 湖南中创化工股份有限公司 | Method for preparing sec-butyl alcohol |
| CN106631689A (en) * | 2015-11-02 | 2017-05-10 | 中国石油化工股份有限公司 | Preparation method for sec-butyl alcohol |
| CN107235824A (en) * | 2017-06-05 | 2017-10-10 | 惠州宇新化工有限责任公司 | A kind of method that isopropyl acetate prepares isopropanol with low-carbon alcohols reaction |
| CN109678670A (en) * | 2017-10-19 | 2019-04-26 | 中国石油化工股份有限公司 | A method of preparing sec-butyl alcohol |
| CN111377802A (en) * | 2018-12-27 | 2020-07-07 | 湖南中创化工股份有限公司 | Preparation method and system of sec-butyl alcohol |
| CN115724715A (en) * | 2022-12-07 | 2023-03-03 | 湖南中创化工股份有限公司 | Sec-butyl alcohol refining method and device |
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| CN102838450A (en) * | 2012-09-20 | 2012-12-26 | 福州大学 | Method for catalyzing synthesizing sec-butyl alcohol through cation exchange resin |
| CN102964243B (en) * | 2012-11-16 | 2017-07-11 | 北京石油化工学院 | The preparation method of sec-Butyl Acetate |
| CN102964243A (en) * | 2012-11-16 | 2013-03-13 | 北京石油化工学院 | Preparation method of sec-butyl acetate |
| CN104311390A (en) * | 2014-10-17 | 2015-01-28 | 深圳市飞扬实业有限公司 | Method for synthesizing sec-butyl alcohol |
| CN104475109A (en) * | 2014-11-20 | 2015-04-01 | 北京恩泽福莱科技有限公司 | Catalyst for preparing sec-butyl alcohol and preparation method of catalyst |
| CN105130745A (en) * | 2015-07-22 | 2015-12-09 | 深圳市前海飞扬新能源科技有限公司 | Method of producing sec-butyl alcohol |
| CN106554275A (en) * | 2015-09-25 | 2017-04-05 | 中国石油化工股份有限公司 | A kind of method comprehensively utilized by C-4-fraction after ether |
| CN106631684A (en) * | 2015-10-31 | 2017-05-10 | 湖南中创化工股份有限公司 | Method for preparing SBA(sec-butyl alcohol) through hydrolysis with sec-butyl acetate |
| CN106631699A (en) * | 2015-10-31 | 2017-05-10 | 湖南中创化工股份有限公司 | Method for preparing sec-butyl alcohol |
| CN106631684B (en) * | 2015-10-31 | 2019-07-16 | 湖南中创化工股份有限公司 | A method of sec-butyl alcohol is prepared with sec-butyl acetate hydrolysis |
| CN106631699B (en) * | 2015-10-31 | 2019-07-16 | 湖南中创化工股份有限公司 | A method of preparing sec-butyl alcohol |
| CN106631689A (en) * | 2015-11-02 | 2017-05-10 | 中国石油化工股份有限公司 | Preparation method for sec-butyl alcohol |
| CN106631689B (en) * | 2015-11-02 | 2019-09-10 | 中国石油化工股份有限公司 | A kind of preparation method of sec-butyl alcohol |
| CN107235824A (en) * | 2017-06-05 | 2017-10-10 | 惠州宇新化工有限责任公司 | A kind of method that isopropyl acetate prepares isopropanol with low-carbon alcohols reaction |
| CN109678670A (en) * | 2017-10-19 | 2019-04-26 | 中国石油化工股份有限公司 | A method of preparing sec-butyl alcohol |
| CN109678670B (en) * | 2017-10-19 | 2022-06-07 | 中国石油化工股份有限公司 | Method for preparing sec-butyl alcohol |
| CN111377802A (en) * | 2018-12-27 | 2020-07-07 | 湖南中创化工股份有限公司 | Preparation method and system of sec-butyl alcohol |
| CN111377802B (en) * | 2018-12-27 | 2022-12-09 | 湖南中创化工股份有限公司 | Preparation method and system of sec-butyl alcohol |
| CN115724715A (en) * | 2022-12-07 | 2023-03-03 | 湖南中创化工股份有限公司 | Sec-butyl alcohol refining method and device |
| CN115724715B (en) * | 2022-12-07 | 2024-03-08 | 湖南中创化工股份有限公司 | Refining method and device of sec-butyl alcohol |
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