CN102452934B - Preparation method of sec-butyl acetate - Google Patents
Preparation method of sec-butyl acetate Download PDFInfo
- Publication number
- CN102452934B CN102452934B CN201010515132.XA CN201010515132A CN102452934B CN 102452934 B CN102452934 B CN 102452934B CN 201010515132 A CN201010515132 A CN 201010515132A CN 102452934 B CN102452934 B CN 102452934B
- Authority
- CN
- China
- Prior art keywords
- tower
- catalytic distillation
- reaction
- sec
- distillation tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a preparation method of sec-butyl acetate. The method is characterized by comprising the following steps: firstly reacting an etherified C4 raw material or an etherified C4 raw material containing inert gases with acetic acid through a fixed bed pre-reaction device; feeding a mixture after pre-reaction into a catalytic distillation tower from the upper part of the reaction section of the catalytic distillation tower, feeding the supplemental etherified C4 raw material or etherified C4 raw material containing inert gases into the catalytic distillation tower from a stripping section at the lower part of the catalytic distillation tower, and carrying out counter-flow contact reaction on two materials at the surface of a catalyst; and enabling unreacted mixed C4 to flow out from the top of the catalytic distillation tower, and enabling the product sec-butyl acetate to flow out from the kettle of the catalytic distillation tower, wherein the fixed bed pre-reaction device and the catalytic distillation tower are filled with the same solid catalyst. By utilizing the method provided by the invention, the acetic acid conversion rate can reach 100%, separation and refinement processes are completed in one catalytic distillation tower, the qualified sec-butyl acetate product can be obtained in the kettle of the tower, the reaction selectivity is high, the separation process is effectively simplified, the process flow is simple, and the manufacturing cost is low.
Description
Technical field
The present invention relates to a kind of preparation method of sec-butyl acetate, particularly a kind of taking carbon four after acetic acid and ether as raw material, the technique preparation that employing fixed bed pre-reactor is combined with catalytic distillation technology and the method for the secondary butyl ester of separating acetic acid.
Background technology
Sec-butyl acetate has the advantages such as environmental protection, low toxicity, solubility property are good as organic solvent, and the n-butyl acetate that alternative price is in the market higher uses.
At present technique majority of catalytic Synthesis of sec-Butyl Acetate is alcohol esterification process, i.e. acetic acid and the sec-butyl alcohol esterification of dewatering under sulphur acid as catalyst condition, but the method separating technology complexity is divided water difficulty; Cause the generation of spent acid using sulfuric acid as catalyzer, not only serious to equipment corrosion, and environment has also been caused to pollution.In recent years, there is bibliographical information to produce sec-butyl acetate by the acid catalyzed reaction of acetic acid and alkene.Compare acid/alcohol method, acid/alkene method can reduce raw materials cost, reduces point water difficulty of acid/alcohol technique existence, the problem that energy consumption is high, belongs to green chemical industry technique.But unstable, easily decomposition that the weak point of the method is used heteropolyacid catalyst; And during using molecular sieve as catalyzer, make reaction yield extremely low because strength of acid is low.
CN10100425A discloses a kind of method of synthesis of acetic acid ester; the propylene of this method employing mol ratio 0.3～3.0 or butylene and acetic acid are raw material; taking solid acid as main body catalyzer, before main body catalyzer, add the pre-protective material of catalyzer, reduce the atom loss in main reaction process.Building-up reactions is carried out at upflow fixed bed reactor, and above-mentioned reaction conditions comprises that temperature of reaction is 50～170 DEG C, and reaction pressure is 0.2～4.0Mpa, and acetic acid air speed is 0.1～4.0
-1.This invention acetic acid transformation efficiency is up to 80%.
CN101121656A provides a kind of method by acetic acid and linear butylene catalytic Synthesis of sec-Butyl Acetate, adopt fixed-bed reactor, use the solid catalysts such as heteropolyacid, modified resin or super acids, generate object product through gas, liquid, solid phase reaction, then obtain sec-butyl acetate product through fractionation and rectifying.Because the heteropolyacid catalyst using has the shortcoming such as unstable, easy decomposition, easy loss, acetic acid low conversion rate, has strengthened the difficulty of industrial enforcement.
CN101735047A relates to a kind of technique of continuous production sec-butyl acetate, and it is that solid-liquid mixing acid is catalyzer taking acetic acid and 1-butylene as raw material, adopts and sprays collision stream tower reactor, the integrated system of the installation compositions such as distillation system and water-and-oil separator.Wherein spray collision and flow tower reactive system mainly by spray-collision stream conversion zone and the tower conversion zone of column plate/filler, pump circulation and the most of formation of observing and controlling part and catalyst change part etc. four.The weak point of this method is that the acetic acid that (1) is used is corrosive, harsher to the requirement of jet apparatus; (2) increase of contact kinetic energy, greatly shorten the work-ing life of catalyzer.
Above-mentioned patent is mainly catalyzer and the reaction process of reacting with C 4 olefin about acetic acid, seldom relates to the separation problem of sec-butyl acetate.For the addition reaction of acetic acid and C 4 olefin, reaction product, except sec-butyl acetate, also has unreacted acetic acid, C 4 olefin, superimposed by product carbon eight alkene etc.; And 118 DEG C of acetic acid boiling points, 113 DEG C of sec-butyl acetates, 101～120 DEG C of carbon eight alkene boiling points, adopt the method for conventional rectification to be difficult to be isolated.Therefore, how separating-purifying sec-butyl acetate product from reaction mixture, is one of key of this technology.
In prior art, CN101130495A proposed a kind of from butylene and acetic acidreaction the method for the secondary butyl ester of separating acetic acid, first adopt flashing tower A separation of C
4and light constituent; Again by the secondary butyl ester of rectifying tower B separating acetic acid and acetic acid; Finally by treating tower C, sec-butyl acetate is refined.Because the boiling point of acetic acid and sec-butyl acetate is close, therefore conventional distillation is difficult to realize both effective separation.
CN101007761A disclose a kind of from the mixture mixed c 4 and acetic acidreaction the method for the secondary butyl ester of separating acetic acid, first by product by flashing tower from tower top separation of C
4and light constituent; Again flashing tower bottom product is separated by the azeotropy rectification column taking water as entrainer; The tower top material of azeotropy rectification column is entered to refining sec-butyl acetate, the purity to 99% of obtaining for the treatment of tower; Wherein azeotropy rectification column materials at bottom of tower can use by direct circulation.This application proposed a kind of from butylene and acetic acidreaction the method for the secondary butyl ester of separating acetic acid, but the weak point of this method is that (1) adopts the method for flash distillation to be difficult to complete separation of carbon four and light constituent; (2) in rectifying, introduce water and caused the reduction of concentration in the use procedure of acetic acid secondary.(3) rectification process long flow path.
CN101486640A reacts the method for preparing sec-butyl acetate with C 4 olefin about acetic acid, under the existence and addition reaction condition of catalyzer, C 4 olefin is contacted, reacted with acetic acid several times.Separating technology comprises a flashing tower, 2 azeotropy rectification columns, needs to add water to carry out azeotropic distillation in rectifying.Although the method adopts azeotropic distillation technique to realize separating of acetic acid and sec-butyl acetate and other organic constituents, technique is comparatively complicated, and energy consumption is higher.
CN101168506A discloses a kind of method of preparing sec-butyl acetate with product separating technique, reacts in catalytic distillation tower with acid and mixed c 4, and reacted product mixtures obtains sec-butyl acetate product through component distillation, rectifying.The method adopts catalytic distillation technology, and product separation has saved flashing tower, but still needs component distillation, and separation circuit is long.
In sum, prior art has the following disadvantages: in (1) sour alkene addition process, one-time reaction transformation efficiency is lower, and the easy inactivation of catalyzer, (2) in product separation process, add water to cause the increase of separation costs, (3) prepare separating technology complexity, seriously polluted.
Summary of the invention
Technical problem to be solved by this invention is to overcome acetic acid low conversion rate in prior art, sec-butyl acetate poor selectivity, the long difficult problem of separation circuit, and the method for the synthetic and secondary butyl ester of separating acetic acid that a kind of synthesis technique flow process is simple, separation circuit is simplified, energy consumption is low, reaction preference is high is provided.
The preparation method of a kind of sec-butyl acetate of the present invention, after the ether that it is characterized in that carbon four raw materials after ether or comprise rare gas element, carbon four raw materials first react by fixed bed pre-reactor with acetic acid, mixture after pre-reaction enters in tower from the top of catalytic distillation tower conversion zone, after the ether of adding, after carbon four raw materials or the ether that comprises rare gas element, carbon four raw materials enter in tower from the bottom stripping section of catalytic distillation tower, two strands of materials react in the surperficial counter current contact of catalyzer, unreacted mixed c 4 flows out from tower top, product sec-butyl acetate flows out from tower reactor, fixed bed pre-reactor and catalytic distillation tower load same solid catalyst.
Wherein preferred technical scheme is:
Described fixed bed pre-reactor can be one, also can adopt multiple.
Described catalytic distillation tower is made up of a tower reactor, stripping section, one or more reaction bed, a rectifying section and a trim the top of column condenser; Be uniform-distribution with the catalytic distillation basket of some amount at reaction bed, the solid catalyst same with fixed bed pre-reactor is housed in catalytic distillation basket.
Described solid catalyst comprises resin catalyst, heteropolyacid catalyst, molecular sieve catalyst.The preferably cation exchange resin catalyst of sulfonic acid series macropore.
Described rare gas element is N
2, one or more mixtures in C02, methane, ethane, propane, Trimethylmethane, butane and pentane.The quality percentage composition of 2-butylene in mixing raw material is 10%～100%, preferably 50%～80%.
The operational condition of fixed bed pre-reactor is: 70～120 DEG C of temperature of reaction, preferably 80～100 DEG C; Reaction pressure 0.8～2.0MPa, preferably 1～1.5Mpa; Air speed 0.2～5h
-1, preferably 0.5～1.5h
-1.After acetic acid and ether, in carbon four, the mol ratio of 2-butylene is 1: 1～1: 3, is preferably 1: 1～1: 1.5, preferably 1: 1～1: 1.2.
In product mixtures after fixed bed pre-reaction, mainly contain sec-butyl acetate, acetic acid, mixed c 4 and light constituent, because acetic acid and sec-butyl acetate boiling-point difference only have 5 DEG C, can greatly simplify sepn process so acetic acid transforms completely.
In technique scheme, can be by adjusting process parameter control esterification reaction process and the product separation of fixed bed pre-reactor and catalytic distillation tower.
In fixed bed pre-reactor, the transformation efficiency of acetic acid can be controlled in 60%～76%, and the mixture after pre-reaction continues to react with carbon after ether four after entering catalytic distillation tower, and unreacted acetic acid transformation efficiency in tower can reach 100%.Because the boiling point of sec-butyl acetate and acetic acid is very approaching, adopt the method for azeotropic distillation two materials effectively could be separated.In catalytic distillation tower, acetic acid transforms completely, has simplified the purification process of product, has reduced energy consumption, and tower reactor can directly obtain qualified sec-butyl acetate product.
Described catalytic distillation tower operational condition is: tower top pressure is 0.35～1.1Mpa, preferably 0.45～1.0Mpa; Tower top temperature is controlled at 40～95 DEG C, preferably 45～65 DEG C; Conversion zone temperature is 65～120 DEG C, preferably 75～90 DEG C; Tower reactor temperature is controlled at 80～150 DEG C, preferably 90～130 DEG C; The reflux ratio of tower is 0.1～10, preferably 0.5～4.
After the ether of adding in catalytic distillation tower, in carbon four, 2-butylene and unreacted acetic acid mol ratio are 1: 1～4: 1, preferably 1: 1～1.8: 1.
Advantage of the present invention:
The preparation method of a kind of sec-butyl acetate of the present invention is different from fixed bed or the catalytic distillation tower reaction of prior art.The technique that the present invention adopts fixed bed pre-reactor to be combined with catalytic distillation technology, by adjusting the processing parameter of fixed bed pre-reactor and catalytic distillation tower, can make acetic acid transformation efficiency reach 100%, in catalytic distillation tower, complete separating of reaction and product, save for the flashing tower except carbon elimination four and light constituent, for separating of azeotropy rectification column and the product rectifying tower of acetic acid, separating technology is simplified, Energy Intensity Reduction, whole reaction conversion ratio is high, technical process is simple, and the sec-butyl acetate purity obtaining is more than 99%.
Embodiment
Below by embodiment, the invention will be further described, but the present invention is not limited only to these examples.Also can fully understand essence of the present invention and invention scope by these embodiment, further understand the feature of synthetic and separating technology of the present invention.
In reaction of the present invention, acetic acid used is the high purity acetic acid of industrial acetic or > 98wt%, and the butylene in reaction is the mixture of 1-butylene, 2-butylene, 1-butylene and 2-butylene and the butylene gas mixture that contains relative inertness gas.
Embodiment 1-7
After mixing the metering in 1: 1 in molar ratio of carbon four (2-butylene mass content 58%) after 98% chemical pure acetic acid and ether, ram pump injects the fixed bed pre-reactor that resin catalyst is housed, mixture through pre-reaction enters in catalytic distillation tower again, and unreacted acetic acid fully reacts with supplementary carbon four.Wherein, after supplementary ether, in carbon four, 2-butylene and unreacted acetic acid mol ratio are 1.2: 1.Fixed bed pre-reactor loaded catalyst is 40ml, and in catalytic distillation tower, loaded catalyst is 100ml.
Test-results under differing temps and air speed condition is as shown in table 1.
Impact on reaction under table 1 differing temps and air speed condition
Can find out, the acetic acid in embodiment 3 transforms completely, and the selectivity of sec-butyl acetate reaches more than 99%.The isolated sec-butyl acetate product of catalytic distillation tower tower reactor is completely qualified.
Embodiment 8-10
The operational condition that fixed bed pre-reactor and catalytic distillation tower adopt, with embodiment 3, changes the reflux ratio of catalytic distillation tower, investigates the impact on reaction, the results are shown in Table 2.
The impact (%) of the different reflux ratios of table 2 on reaction
As can be seen here, along with the increase of reflux ratio, the selectivity of ester can be brought up to more than 99%.
Embodiment 11-13
Fixed bed pre-reactor and catalytic distillation tower adopt 3 operational condition, change the impact of pressure on reaction, and test-results is in table 3.
The impact of table 3 different pressures on reaction
Embodiment 14-16
, enter again in catalytic distillation tower and fully react with supplementary carbon four through the mixture of pre-reaction injecting the fixed bed pre-reactor that heteropolyacid catalyst is housed after the metering in 1: 1 in molar ratio of carbon four (2-butylene mass content 58%) after 98% chemical pure acetic acid and ether through ram pump.Wherein, after supplementary ether, in carbon four, 2-butylene and unreacted acetic acid mol ratio are 1.2: 1.Fixed bed pre-reactor loaded catalyst is 40ml, and in catalytic distillation tower, loaded catalyst is 100ml.Test-results is as shown in table 4.
The impact of table 4 heteropolyacid catalyst on reaction result
As can be seen from Table 4, adopt the catalyzer of heteropolyacid as reaction, acetic acid low conversion rate, and catalyzer is easy to inactivation in reaction process.
Comparative example 17-19
Through ram pump, 98% chemical pure acetic acid is injected in tower from the top of catalytic distillation tower conversion zone, after ether, carbon four injects in tower from the bottom stripping section of catalytic distillation tower, the raw materials components mole ratio of acetic acid and carbon four (2-butylene mass content 58%) is 1: 1.1, acetic acid feed amount is 25ml/h, in tower, loaded catalyst is 100ml, and esterification the results are shown in Table 5.
The reaction result of table 5 catalytic distillation tower
As can be seen from Table 5, only use catalytic distillation device, although acetic acid transformation efficiency is higher, how Optimizing operation all can not make acetic acid transform completely, obtain highly purified sec-butyl acetate product, later separation complex procedures.
Claims (4)
1. the preparation method of a sec-butyl acetate, after the ether that it is characterized in that carbon four raw materials after ether or comprise rare gas element, carbon four raw materials first react by fixed bed pre-reactor with acetic acid, mixture after pre-reaction enters in tower from the top of catalytic distillation tower conversion zone, after the ether of adding, after carbon four raw materials or the ether that comprises rare gas element, carbon four raw materials enter in tower from the bottom stripping section of catalytic distillation tower, two strands of materials react in the surperficial counter current contact of catalyzer, unreacted mixed c 4 flows out from tower top, product sec-butyl acetate flows out from tower reactor, fixed bed pre-reactor and catalytic distillation tower load same solid catalyst, described solid catalyst is resin catalyst,
The operational condition of described fixed bed pre-reactor is: 80 DEG C of temperature of reaction, reaction pressure 1.0MPa, air speed 1 h
-1, after acetic acid and ether, in carbon four, the mol ratio of 2-butylene is 1:1;
The operational condition of described catalytic distillation tower is: working pressure is 0.9MPa, tower top temperature is controlled at 49 DEG C, conversion zone temperature is 87 DEG C, tower reactor temperature is controlled at 115 DEG C, the reflux ratio of tower is 2～4, and after the ether of adding in catalytic distillation tower, in carbon four raw materials, 2-butylene and unreacted acetic acid mol ratio are 1.2:1.
2. the preparation method of sec-butyl acetate according to claim 1, is characterized in that described solid catalyst adopts the cation exchange resin catalyst of sulfonic acid series macropore.
3. the preparation method of sec-butyl acetate according to claim 1, is characterized in that described rare gas element is N
2, CO
2, one or more mixtures in methane, ethane, propane, Trimethylmethane, butane and pentane, the quality percentage composition that the 2-butylene after ether in carbon four accounts for mixing raw material is 50%～80%.
4. the preparation method of sec-butyl acetate according to claim 1, it is characterized in that fixed bed pre-reactor can be one, also can adopt multiple, described catalytic distillation tower is made up of a tower reactor, stripping section, one or more reaction bed, a rectifying section and a trim the top of column condenser, be uniform-distribution with the catalytic distillation basket of some amount at reaction bed, the solid catalyst same with fixed bed pre-reactor is housed in catalytic distillation basket.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010515132.XA CN102452934B (en) | 2010-10-22 | 2010-10-22 | Preparation method of sec-butyl acetate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010515132.XA CN102452934B (en) | 2010-10-22 | 2010-10-22 | Preparation method of sec-butyl acetate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102452934A CN102452934A (en) | 2012-05-16 |
| CN102452934B true CN102452934B (en) | 2014-08-06 |
Family
ID=46036666
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010515132.XA Active CN102452934B (en) | 2010-10-22 | 2010-10-22 | Preparation method of sec-butyl acetate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102452934B (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103508884B (en) * | 2012-06-15 | 2015-09-16 | 中国石油化工股份有限公司 | One utilizes C after ether 4cut prepares the method for 2-butyl acetate |
| CN103508885B (en) * | 2012-06-27 | 2015-10-07 | 中国石油化工股份有限公司 | One utilizes C after ether 4cut prepares the method for 2-butyl acetate |
| CN104529769A (en) * | 2014-12-03 | 2015-04-22 | 江门谦信化工发展有限公司 | Constant-molar-ratio method for producing butyl acrylate crude ester |
| CN106977398A (en) * | 2017-04-21 | 2017-07-25 | 福州大学 | A kind of synthetic method of sec-butyl acetate |
| CN108329207B (en) * | 2018-05-03 | 2023-12-26 | 凯瑞环保科技股份有限公司 | Device and method for producing fatty acid methyl ester by catalytic distillation technology |
| CN114213243A (en) * | 2021-12-03 | 2022-03-22 | 王义成 | Production system and method of sec-butyl acetate |
| CN115784879A (en) * | 2022-11-24 | 2023-03-14 | 凯瑞环保科技股份有限公司 | Synthesis method of sec-butyl acetate |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5457228A (en) * | 1990-10-31 | 1995-10-10 | Daicel Chemical Industries, Ltd. | Method for producing lower alkyl acetate |
| CN101143819A (en) * | 2007-10-16 | 2008-03-19 | 胡先念 | Method for preparing sec-butyl acetate |
| CN101168505A (en) * | 2007-11-30 | 2008-04-30 | 胡先念 | Preparation method for sec-butyl acetate with product separating and reclaiming technique |
| CN101168506A (en) * | 2007-11-30 | 2008-04-30 | 胡先念 | Preparation method for sec-butyl acetate with product separating technique |
| CN101481306A (en) * | 2009-01-13 | 2009-07-15 | 湖南瑞源石化股份有限公司 | Preparation of lower fatty acid ester and apparatus for preparing lower fatty acid ester |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7253305B2 (en) * | 2005-07-26 | 2007-08-07 | Lyondell Chemical Technology, L.P. | Tertiary alkyl acetate preparation |
-
2010
- 2010-10-22 CN CN201010515132.XA patent/CN102452934B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5457228A (en) * | 1990-10-31 | 1995-10-10 | Daicel Chemical Industries, Ltd. | Method for producing lower alkyl acetate |
| CN101143819A (en) * | 2007-10-16 | 2008-03-19 | 胡先念 | Method for preparing sec-butyl acetate |
| CN101168505A (en) * | 2007-11-30 | 2008-04-30 | 胡先念 | Preparation method for sec-butyl acetate with product separating and reclaiming technique |
| CN101168506A (en) * | 2007-11-30 | 2008-04-30 | 胡先念 | Preparation method for sec-butyl acetate with product separating technique |
| CN101481306A (en) * | 2009-01-13 | 2009-07-15 | 湖南瑞源石化股份有限公司 | Preparation of lower fatty acid ester and apparatus for preparing lower fatty acid ester |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102452934A (en) | 2012-05-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102452934B (en) | Preparation method of sec-butyl acetate | |
| EP4049748A1 (en) | Gas-liquid bubbling bed reactor, reaction system and method for synthesizing carbonate | |
| CN110372512B (en) | Separation and purification process of dimethyl carbonate | |
| CN100463897C (en) | Method for separating sec-butyl acetate from reaction mixture of acetic acid and hybrid C4 | |
| CN109456190A (en) | A kind of method of the continuous synthesizing propylene glycol monomethyl ether acetate of the highly selective catalytic distillation of low temperature | |
| CN106631684A (en) | Method for preparing SBA(sec-butyl alcohol) through hydrolysis with sec-butyl acetate | |
| CN105111079A (en) | Method and device for separating acetic acid sec-butyl ester and sec-butyl alcohol | |
| CN113683483B (en) | Production method and device of high-purity 1, 6-hexanediol | |
| CN101168505B (en) | Preparation method for sec-butyl acetate with product separating and reclaiming technique | |
| CN102557932A (en) | Method for producing isobutyl acetate | |
| CN102134191A (en) | Process method for producing ethyl acetate by catalytic rectification | |
| CN105461515A (en) | Method for preparing cyclopentanol from cyclopentene | |
| CN108947774B (en) | Method and device for separating isopropanol | |
| CN1903828A (en) | Process for producing dimethyl carbonate by urea alcoholysis method | |
| CN110172013B (en) | Process for synthesizing tertiary amyl alcohol based on catalytic distillation solvent method | |
| CN101429099B (en) | Method for producing dichlorohydrin with glycerol | |
| CN101168506B (en) | Preparation method for sec-butyl acetate with product separating technique | |
| CN106588597A (en) | Method for purifying polyoxyethene dimethyl ether | |
| CN103664520A (en) | Method for preparing isopropyl alcohol through hydration reaction of propylene | |
| CN113548967A (en) | Device and method for producing high-purity dimethyl carbonate by heterogeneous catalytic reaction rectification | |
| CN113480430A (en) | Device and method for producing high-purity dimethyl carbonate by catalytic extraction rectification | |
| CN102976939B (en) | Preparation method of propionate | |
| CN110668920A (en) | Method for preparing ethanol and co-producing cyclohexanol by using reactive distillation method | |
| CN209906679U (en) | Device for preparing methyl formate by catalytic distillation | |
| CN87105641A (en) | Produce Virahol and have the method for the tertiary alcohols of 4 to 5 carbon atoms |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |