CN101007761A - Method for separating sec-butyl acetate from reaction mixture of acetic acid and hybrid C4 - Google Patents
Method for separating sec-butyl acetate from reaction mixture of acetic acid and hybrid C4 Download PDFInfo
- Publication number
- CN101007761A CN101007761A CN 200710200148 CN200710200148A CN101007761A CN 101007761 A CN101007761 A CN 101007761A CN 200710200148 CN200710200148 CN 200710200148 CN 200710200148 A CN200710200148 A CN 200710200148A CN 101007761 A CN101007761 A CN 101007761A
- Authority
- CN
- China
- Prior art keywords
- acetate
- controlled
- tower
- sec
- entrainer
- 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.)
- Granted
Links
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 title claims abstract description 39
- 238000000034 method Methods 0.000 title claims abstract description 22
- DCKVNWZUADLDEH-UHFFFAOYSA-N sec-butyl acetate Chemical compound CCC(C)OC(C)=O DCKVNWZUADLDEH-UHFFFAOYSA-N 0.000 title claims description 68
- 239000011541 reaction mixture Substances 0.000 title description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 30
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 claims description 63
- 239000000463 material Substances 0.000 claims description 44
- 238000010533 azeotropic distillation Methods 0.000 claims description 27
- 241000282326 Felis catus Species 0.000 claims description 20
- 238000007701 flash-distillation Methods 0.000 claims description 19
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical group C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 15
- 238000000605 extraction Methods 0.000 claims description 11
- 239000000470 constituent Substances 0.000 claims description 8
- 239000012451 post-reaction mixture Substances 0.000 claims description 8
- 230000003116 impacting effect Effects 0.000 claims description 7
- 238000006243 chemical reaction Methods 0.000 claims description 6
- 239000003054 catalyst Substances 0.000 claims description 5
- 230000000694 effects Effects 0.000 claims description 5
- 230000003245 working effect Effects 0.000 claims description 5
- JMMWKPVZQRWMSS-UHFFFAOYSA-N isopropanol acetate Chemical group CC(C)OC(C)=O JMMWKPVZQRWMSS-UHFFFAOYSA-N 0.000 claims description 4
- 229940011051 isopropyl acetate Drugs 0.000 claims description 4
- GWYFCOCPABKNJV-UHFFFAOYSA-N isovaleric acid Chemical group CC(C)CC(O)=O GWYFCOCPABKNJV-UHFFFAOYSA-N 0.000 claims description 4
- 238000009834 vaporization Methods 0.000 claims description 3
- 230000008016 vaporization Effects 0.000 claims description 3
- 150000004945 aromatic hydrocarbons Chemical group 0.000 claims description 2
- 150000002148 esters Chemical group 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- 239000002253 acid Substances 0.000 abstract description 5
- 125000000484 butyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 abstract 2
- 150000001875 compounds Chemical class 0.000 abstract 1
- 238000004064 recycling Methods 0.000 abstract 1
- 229930195733 hydrocarbon Natural products 0.000 description 23
- 150000002430 hydrocarbons Chemical class 0.000 description 23
- 238000000746 purification Methods 0.000 description 11
- 238000009835 boiling Methods 0.000 description 8
- 239000000203 mixture Substances 0.000 description 6
- 238000000926 separation method Methods 0.000 description 4
- 239000000758 substrate Substances 0.000 description 4
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 3
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 3
- 239000002994 raw material Substances 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 1
- 238000007036 catalytic synthesis reaction Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a separating method of butyl para-acetate from the reacted compound of acetic acid and C4, which comprises the following steps: flashing to remove non-reacted C4 and light component; flowing production from the bottom of flashing tower into coboiling rectifying tower; adding coboiler A to separate butyl para-acetate and acetic acid; transmitting mass from coboiler into acid condensing tower; adding coboiler B to coboil and rectify again; condensing acetic acid; obtaining the product with purity over 99% and acetic acid content less than 0.01% and water less than 0.05%; recycling acetic acid.
Description
Technical field
The present invention relates to a kind of from acetate and hybrid C 4 post reaction mixture the method for the secondary butyl ester of separating acetic acid.
Background technology
For traditional technology, utilize 1-butylene, 2-butylene to have for raw material and acetic acidreaction prepare sec-butyl acetate that raw material sources are wide and inexpensive, good in economic efficiency, advantages of environment protection, therefore, its synthesising process research has obtained extensive concern.
But utilize the research of the separation and purification technology of acetate and 1-butylene, 2-butylene prepared in reaction sec-butyl acetate to report less.
US5457228 has reported a kind of method of utilizing acetate and 1-butylene and 2-butylene reaction catalytic Synthesis of sec-Butyl Acetate, and olefin conversion that obtains and selectivity of product are all higher.For its separation method, mention in the patent and utilize distillation just sec-butyl acetate can be separated from reaction mixture.But patent is not announced concrete separation method, does not announce after separating the purity that product reached yet.
But the boiling point of sec-butyl acetate and acetate is very approaching, therefore, utilizes simple distillating method to be difficult to sec-butyl acetate is fully separated with acetate.
Summary of the invention
The purpose of this invention is to provide a kind of from acetate and hybrid C 4 post reaction mixture the method for the secondary butyl ester of separating acetic acid.
Mainly contain sec-butyl acetate, acetate, hybrid C 4 and light constituent in acetate and the hybrid C 4 post reaction mixture.
For achieving the above object, adopt following technical scheme:
(1) acetate and hybrid C 4 post reaction mixture enter flashing tower, by flash distillation from unreacted hybrid C 4 of flash distillation removed overhead and light constituent;
(2) the flashing tower bottom product enters azeotropy rectification column, adds entrainer A, by azeotropic distillation with sec-butyl acetate and separated from acetic acid;
(3) azeotropic distillation cat head material enters treating tower, obtains sec-butyl acetate by rectifying;
(4) amount that contains entrainer A when acetate from the extraction of azeotropy rectification column bottom to reaction impact or to catalyst activity with when impacting work-ing life, azeotropy rectification column bottom material enters sour upgrading tower, add entrainer B, through azeotropic distillation again, acetate is concentrated acetate recycle after concentrating; Or: the amount that contains entrainer A when the acetate from the extraction of azeotropy rectification column bottom can be to not impacting of reacting, and in the time of also can and not impacting work-ing life catalyst activity, azeotropy rectification column bottom material directly loops back reactive system and utilizes.
In the mixture that contains sec-butyl acetate, acetate, hybrid C 4 and light constituent, because the boiling point of hybrid C 4 and light constituent is far below the boiling point of sec-butyl acetate and acetate, therefore, can steam hybrid C 4 and other light constituent from the flash distillation cat head, obtain sec-butyl acetate and acetate at the bottom of the tower by flash distillation.
In flash vaporization process, the flashing tower bottom temp should be controlled at 140～220 ℃, preferred 170～190 ℃.Be higher than 220 ℃ as temperature, easily sec-butyl acetate and acetate steamed the flash distillation cat head; Be lower than 140 ℃ as temperature, then unreacted C4 component and other light constituent can not steam the flash distillation cat head fully.
The flashing tower head temperature should be controlled at 40～90 ℃, preferred 50～70 ℃; Flashing tower roof pressure Etech is controlled at 0.30～1.20MPa, preferred 0.35～0.75MPa.Its objective is that the C4 component and other light constituent that make the flash distillation cat head keep liquid.
Because the boiling point of sec-butyl acetate and acetate is very approaching, therefore, need utilize the method for azeotropic distillation sec-butyl acetate effectively could be separated with acetate.The invention provides a kind of entrainer A, utilize itself and sec-butyl acetate to form azeotrope, and the boiling point of the boiling point of its azeotrope and acetate differs bigger characteristics, can be with sec-butyl acetate fully separation from acetate.
The azeotropic distillation column bottom temperature should be controlled at 100～130 ℃, preferred 105～125 ℃.Be higher than 130 ℃ as temperature, then acetate can enter cat head; Be lower than 100 ℃ as temperature, the azeotrope of sec-butyl acetate and entrainer A then can not effectively steam cat head.Azeotropic distillation cat head temperature should be controlled at 80～100 ℃, preferred 80～90 ℃.
Entrainer A is that any one can form azeotrope with sec-butyl acetate, and the boiling point of its azeotropic point and acetate differs the material more than 10 ℃.Among the present invention, entrainer A is selected from water.
After sec-butyl acetate and entrainer A steam from the azeotropic distillation cat head, through cooling, sec-butyl acetate and entrainer A natural layering.Entrainer A passes back into the azeotropic distillation cat head, and the sec-butyl acetate of carrying a small amount of entrainer A secretly then enters treating tower, obtains highly purified sec-butyl acetate by rectifying.
The product purification column bottom temperature should be controlled at 115～135 ℃, preferred 118～125 ℃.Be higher than 135 ℃ as temperature, then have a large amount of product sec-butyl acetates to steam cat head, output is reduced; Be lower than 115 ℃ as temperature, partial impurities can not be separated from product, has reduced the quality of product.Product purification top of tower temperature should be controlled at and be not less than 87 ℃, preferably is not less than 95 ℃.
Acetate and a small amount of entrainer A and/or sec-butyl acetate are then from the extraction of azeotropy rectification column bottom.Measure bigger when the acetate from the extraction of azeotropy rectification column bottom contains entrainer A, can to reaction impact or to catalyst activity with when impacting work-ing life, material is sent into the acetate concentration tower, and in system, add entrainer B, make itself and entrainer A form azeotrope, and this azeotrope is steamed.
Acid upgrading tower bottom temp should be controlled at 100～130 ℃, preferred 115～125 ℃.Be higher than 130 ℃ as temperature, then acetate can enter cat head; Be lower than 100 ℃ as temperature, the azeotrope of entrainer A and entrainer B then can not effectively steam cat head.
Entrainer B is that any one can form azeotrope with entrainer A, and the boiling point of its azeotropic point and acetate differs the material more than 10 ℃.Among the present invention, entrainer B is selected from Ester, aromatic hydrocarbons, preferred sec-butyl acetate, isopropyl acetate, benzene.
When the acetate from the extraction of azeotropy rectification column bottom contains entrainer A amount less than 5% (quality percentage composition), can not carry out acetate and concentrate, directly with the acetate recycle.
The invention has the advantages that and sec-butyl acetate can be separated from acetate and hybrid C 4 post reaction mixture that the purity of the sec-butyl acetate that obtains is more than 99%, quality of acetic acid content is less than 0.01%, and quality content is less than 0.05%; The acetate reusable edible.
Embodiment
The present invention is further illustrated by the following examples, but content not thereby limiting the invention.
Embodiment 1: the mixture input flashing tower that quality group is become sec-butyl acetate 45.03%, acetate 37.29%, hydro carbons and other material 17.68%.The flash distillation column bottom temperature is 180.5 ℃, and the flash distillation tower top temperature is 56 ℃, and pressure is 0.65MPa.Obtaining flashing tower bottom product quality group becomes: sec-butyl acetate 52.21%, acetate 43.24%, hydro carbons and other material 4.55%.
Flashing tower substrate material enters azeotropy rectification column, and simultaneously in sec-butyl acetate: the ratio of water=4: 1 (mass percent) adds entrainer water in azeotropy rectification column.The azeotropic distillation column bottom temperature is 125 ℃, and tower top temperature is 87.5 ℃.Obtaining the overhead product quality group becomes: sec-butyl acetate 94.07%, acetate 0.1%, hydro carbons and other material 4.83%, water 1.0%.Extraction fractions consisting in tower bottom is: sec-butyl acetate 6.39%, acetate 89.33%, hydro carbons and other material 3.24%, water 0.69%.
Azeotropic distillation cat head material removes the product purification tower.121 ℃ of product purification column bottom temperature, 107 ℃ of head temperature.Obtaining the bottom product overhead product consists of: sec-butyl acetate 99.1%, acetate 0.007%, water 0.04%, hydro carbons and other material 0.75%.
Azeotropic distillation bottoms material loops back reactive system.
Embodiment 2: the mixture input flashing tower that quality group is become sec-butyl acetate 51.38%, acetate 36.10%, hydro carbons and other material 12.52%.The flash distillation column bottom temperature is 165 ℃, and the flash distillation tower top temperature is 77 ℃, and pressure is 0.48MPa.Obtaining flashing tower bottom product quality group becomes: sec-butyl acetate 55.98%, acetate 40.29%, hydro carbons and other material 3.73%.
Flashing tower substrate material enters azeotropy rectification column, and simultaneously in sec-butyl acetate: the ratio of water=4: 1 (mass percent) adds entrainer water in azeotropy rectification column.The azeotropic distillation column bottom temperature is 115 ℃, and tower top temperature is 82.5 ℃.Obtaining the overhead product quality group becomes: sec-butyl acetate 95.13%, acetate 0.04%, hydro carbons and other material 3.83%, water 1.0%.Extraction fractions consisting in tower bottom is: sec-butyl acetate 8.39%, acetate 81.27%, hydro carbons and other material 4.21%, water 6.13%.
Azeotropic distillation cat head material removes the product purification tower.118 ℃ of product purification column bottom temperature, 101 ℃ of head temperature.Obtaining the bottom product overhead product consists of: sec-butyl acetate 98.24%, acetate 0.005%, water 0.04%, hydro carbons and other material 0.96%.
Azeotropic distillation bottoms material disacidify upgrading tower, simultaneously in sec-butyl acetate: the ratio of water=4: 1 (mass percent) adds the entrainer sec-butyl acetate in azeotropy rectification column.Temperature is 119 ℃ at the bottom of the acid upgrading tower.Obtaining the bottom production consists of: sec-butyl acetate 4.31%, acetate 92.24%, hydro carbons and other material 3.10%, water 0.35%.Production loops back reactor herein.
Embodiment 3: the mixture input flashing tower that quality group is become sec-butyl acetate 44.98%, acetate 36.53%, hydro carbons and other material 18.49%.The flash distillation column bottom temperature is 188 ℃, and the flash distillation tower top temperature is 57 ℃, and pressure is 0.56MPa.Obtaining flashing tower bottom product quality group becomes: sec-butyl acetate 52.49%, acetate 42.78%, hydro carbons and other material 4.73%.
Flashing tower substrate material enters azeotropy rectification column, and simultaneously in sec-butyl acetate: the ratio of water=4: 1 (mass percent) adds entrainer water in azeotropy rectification column.The azeotropic distillation column bottom temperature is 121 ℃, and tower top temperature is 86.5 ℃.Obtaining the overhead product quality group becomes: sec-butyl acetate 94.84%, acetate 0.07%, hydro carbons and other material 4.09%, water 1.0%.Extraction fractions consisting in tower bottom is: sec-butyl acetate 12.10%, acetate 77.69%, hydro carbons and other material 4.28%, water 5.93%.
Azeotropic distillation cat head material removes the product purification tower.122 ℃ of product purification column bottom temperature, 105 ℃ of head temperature.Obtaining the bottom product overhead product consists of: sec-butyl acetate 98.14%, acetate 0.006%, water 0.05%, hydro carbons and other material 1.80%.
Azeotropic distillation bottoms material disacidify upgrading tower, simultaneously in isopropyl acetate: the ratio of water=94: 6 (mass percent) adds the entrainer sec-butyl acetate in azeotropy rectification column.Temperature is 119 ℃ at the bottom of the acid upgrading tower.Obtaining the bottom production consists of: sec-butyl acetate 5.96%, acetate 91.01%, hydro carbons and other material 2.76%, water 0.27%.Production loops back reactor herein.
Embodiment 4: the mixture input flashing tower that quality group is become sec-butyl acetate 44.98%, acetate 36.53%, hydro carbons and other material 18.49%.The flash distillation column bottom temperature is 188 ℃, and the flash distillation tower top temperature is 57 ℃, and pressure is 0.56MPa.Obtaining flashing tower bottom product quality group becomes: sec-butyl acetate 52.49%, acetate 42.78%, hydro carbons and other material 4.73%.
Flashing tower substrate material enters azeotropy rectification column, and simultaneously in sec-butyl acetate: the ratio of water=4: 1 (mass percent) adds entrainer water in azeotropy rectification column.The azeotropic distillation column bottom temperature is 121 ℃, and tower top temperature is 86.5 ℃.Obtaining the overhead product quality group becomes: sec-butyl acetate 94.84%, acetate 0.07%, hydro carbons and other material 4.09%, water 1.0%.Extraction fractions consisting in tower bottom is: sec-butyl acetate 12.10%, acetate 77.69%, hydro carbons and other material 4.28%, water 5.93%.
Azeotropic distillation cat head material removes the product purification tower.122 ℃ of product purification column bottom temperature, 105 ℃ of head temperature.Obtaining the bottom product overhead product consists of: sec-butyl acetate 98.14%, acetate 0.006%, water 0.05%, hydro carbons and other material 1.80%.
Azeotropic distillation bottoms material disacidify upgrading tower, simultaneously in benzene: the ratio of water=91: 9 (mass percent) adds the entrainer sec-butyl acetate in azeotropy rectification column.Temperature is 125 ℃ at the bottom of the acid upgrading tower.Obtaining the bottom production consists of: sec-butyl acetate 5.34%, acetate 91.42%, hydro carbons and other material 2.88%, water 0.33%, benzene 0.03%.Production loops back reactor herein.
Claims (10)
1. the method for the secondary butyl ester of separating acetic acid from acetate and hybrid C 4 post reaction mixture,
It is characterized in that:
(1) acetate and hybrid C 4 post reaction mixture enter flashing tower, by flash distillation from unreacted hybrid C 4 of flash distillation removed overhead and light constituent;
(2) the flashing tower bottom product enters azeotropy rectification column, adds entrainer A, by azeotropic distillation with sec-butyl acetate and separated from acetic acid;
(3) azeotropic distillation cat head material enters treating tower, obtains sec-butyl acetate by rectifying;
(4) amount that contains entrainer A when acetate from the extraction of azeotropy rectification column bottom to reaction impact or to catalyst activity with when impacting work-ing life, azeotropy rectification column bottom material enters sour upgrading tower, add entrainer B, through azeotropic distillation again, acetate is concentrated acetate recycle after concentrating; Or: the amount that contains entrainer A when the acetate from the extraction of azeotropy rectification column bottom can be to not impacting of reacting, and in the time of also can and not impacting work-ing life catalyst activity, azeotropy rectification column bottom material directly loops back reactive system and utilizes.
2. according to the described method of claim 1, it is characterized in that in flash vaporization process, the flashing tower bottom temp is controlled at 140～220 ℃; The flashing tower head temperature is controlled at 40～90 ℃; The flash distillation tower top pressure is controlled at 0.30～1.20MPa.
3. according to the described method of claim 1, it is characterized in that in flash vaporization process, the flashing tower bottom temp is controlled at 170～190 ℃; The flashing tower head temperature is controlled at 50～70 ℃; The flash distillation tower top pressure is controlled at 0.35～0.75MPa.
4. according to claim 1 or 2 described methods, it is characterized in that the azeotropic distillation column bottom temperature is controlled at 100～130 ℃; Azeotropic distillation cat head temperature is controlled at 80～100 ℃; Entrainer A is selected from water.
5. according to the described method of claim 3, it is characterized in that the azeotropic distillation column bottom temperature is controlled at 105～125 ℃; Azeotropic distillation cat head temperature should be controlled at 80～90 ℃; Entrainer A is selected from water.
6. according to claim 1 or 2 described methods, it is characterized in that the treating tower bottom temp is controlled at 115～135 ℃; The treating tower head temperature is controlled at and is not less than 87 ℃.
7. according to the described method of claim 3, it is characterized in that the treating tower bottom temp is controlled at 118～125 ℃; The treating tower head temperature is controlled at and is not less than 95 ℃.
8. according to claim 1 or 2 described methods, it is characterized in that sour upgrading tower bottom temp is controlled at 100～130 ℃, preferred 115～125 ℃; Entrainer B is selected from Ester, aromatic hydrocarbons.
9. according to claim 1 or 2 described methods, it is characterized in that sour upgrading tower bottom temp is controlled at 115～125 ℃; Entrainer B is selected from sec-butyl acetate, isopropyl acetate, benzene.
10. according to claim 1 or 3 or 5 or 7 described methods, it is characterized in that sour upgrading tower bottom temp is controlled at 115～125 ℃; Entrainer B is selected from sec-butyl acetate, isopropyl acetate, benzene.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200710200148XA CN100463897C (en) | 2007-02-02 | 2007-02-02 | A method for separating sec-butyl acetate from the mixture after the reaction of acetic acid and mixed C4 |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200710200148XA CN100463897C (en) | 2007-02-02 | 2007-02-02 | A method for separating sec-butyl acetate from the mixture after the reaction of acetic acid and mixed C4 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101007761A true CN101007761A (en) | 2007-08-01 |
| CN100463897C CN100463897C (en) | 2009-02-25 |
Family
ID=38696465
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB200710200148XA Active CN100463897C (en) | 2007-02-02 | 2007-02-02 | A method for separating sec-butyl acetate from the mixture after the reaction of acetic acid and mixed C4 |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100463897C (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009033381A1 (en) | 2007-09-14 | 2009-03-19 | Hunan Zhongchuang Chemical Co., Ltd | A process of removing heavier hydrocarbons from the reaction products of producing sec-butyl acetate |
| CN101486640B (en) * | 2009-01-13 | 2010-05-12 | 湖南瑞源石化股份有限公司 | A kind of preparation method of sec-butyl acetate |
| CN101481307B (en) * | 2009-01-13 | 2010-06-02 | 湖南瑞源石化股份有限公司 | Method for separating acetic acid and sec-butyl acetate from reaction products |
| CN101168505B (en) * | 2007-11-30 | 2010-06-09 | 湖南中创化工有限责任公司 | Preparation method for sec-butyl acetate with product separating and reclaiming technique |
| CN102584575A (en) * | 2011-01-17 | 2012-07-18 | 胡先念 | Method for refining sec-butyl acetate coarse products through dual-reflux and preparation method of sec-butyl acetate |
| CN102911045A (en) * | 2012-10-19 | 2013-02-06 | 胡先念 | Method for recovering latent heat in sec-butyl acetate preparation device and combined device |
| CN102964244A (en) * | 2012-11-16 | 2013-03-13 | 北京石油化工学院 | Method for separating refined sec-butyl acetate |
| CN104311416A (en) * | 2014-09-03 | 2015-01-28 | 安徽中草香料有限公司 | Method for processing wastes generated during butyl butyryl lactate production process |
| CN104109088B (en) * | 2014-06-23 | 2016-08-17 | 山东胜通集团股份有限公司 | Sec-Butyl Acetate production line |
| CN107151562A (en) * | 2016-03-04 | 2017-09-12 | 中国石油大学(北京) | A kind of method of liquefied gas esterification production high-knock rating gasoline blend component |
| CN115888742A (en) * | 2022-12-15 | 2023-04-04 | 湖南中创化工股份有限公司 | Water-resistant catalyst for hydrogenation of sec-butyl acetate containing water, and preparation method and application thereof |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5384426A (en) * | 1992-12-08 | 1995-01-24 | Daicel Chemical Industries, Ltd. | Process for the preparation of isopropyl acetate |
| GB0120989D0 (en) * | 2001-08-30 | 2001-10-24 | Bp Chem Int Ltd | Process for treating a mixed c4 stream comprising iso-butene and 1,3-butadiene |
| RU2199521C1 (en) * | 2001-09-10 | 2003-02-27 | Закрытое акционерное общество фирма "Альен" | Sec-butyl acetate production process |
-
2007
- 2007-02-02 CN CNB200710200148XA patent/CN100463897C/en active Active
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20100305355A1 (en) * | 2007-09-14 | 2010-12-02 | Hunan Zhongchuang Chemical Co., Ltd. | Method of removing heavy hydrocarbons from reaction products in the production of sec-butyl acetate |
| US8373003B2 (en) * | 2007-09-14 | 2013-02-12 | Hunan Zhongchuang Chemical Co., Ltd. | Method of removing heavy hydrocarbons from reaction products in the production of sec-butyl acetate |
| WO2009033381A1 (en) | 2007-09-14 | 2009-03-19 | Hunan Zhongchuang Chemical Co., Ltd | A process of removing heavier hydrocarbons from the reaction products of producing sec-butyl acetate |
| CN101168505B (en) * | 2007-11-30 | 2010-06-09 | 湖南中创化工有限责任公司 | Preparation method for sec-butyl acetate with product separating and reclaiming technique |
| CN101486640B (en) * | 2009-01-13 | 2010-05-12 | 湖南瑞源石化股份有限公司 | A kind of preparation method of sec-butyl acetate |
| CN101481307B (en) * | 2009-01-13 | 2010-06-02 | 湖南瑞源石化股份有限公司 | Method for separating acetic acid and sec-butyl acetate from reaction products |
| CN102584575B (en) * | 2011-01-17 | 2013-07-17 | 惠州中创化工有限责任公司 | Method for refining sec-butyl acetate coarse products through dual-reflux and preparation method of sec-butyl acetate |
| CN102584575A (en) * | 2011-01-17 | 2012-07-18 | 胡先念 | Method for refining sec-butyl acetate coarse products through dual-reflux and preparation method of sec-butyl acetate |
| CN102911045A (en) * | 2012-10-19 | 2013-02-06 | 胡先念 | Method for recovering latent heat in sec-butyl acetate preparation device and combined device |
| CN102964244A (en) * | 2012-11-16 | 2013-03-13 | 北京石油化工学院 | Method for separating refined sec-butyl acetate |
| CN102964244B (en) * | 2012-11-16 | 2017-04-05 | 北京石油化工学院 | The separation method of refined sec-Butyl Acetate |
| CN104109088B (en) * | 2014-06-23 | 2016-08-17 | 山东胜通集团股份有限公司 | Sec-Butyl Acetate production line |
| CN104311416A (en) * | 2014-09-03 | 2015-01-28 | 安徽中草香料有限公司 | Method for processing wastes generated during butyl butyryl lactate production process |
| CN107151562A (en) * | 2016-03-04 | 2017-09-12 | 中国石油大学(北京) | A kind of method of liquefied gas esterification production high-knock rating gasoline blend component |
| CN107151562B (en) * | 2016-03-04 | 2019-09-17 | 中国石油大学(北京) | A kind of method of liquefied gas esterification production high-knock rating gasoline blend component |
| CN115888742A (en) * | 2022-12-15 | 2023-04-04 | 湖南中创化工股份有限公司 | Water-resistant catalyst for hydrogenation of sec-butyl acetate containing water, and preparation method and application thereof |
| CN115888742B (en) * | 2022-12-15 | 2025-05-06 | 湖南中创化工股份有限公司 | A water-resistant catalyst for hydrogenation of aqueous sec-butyl acetate and its preparation method and application |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100463897C (en) | 2009-02-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101007761A (en) | Method for separating sec-butyl acetate from reaction mixture of acetic acid and hybrid C4 | |
| RU2591703C2 (en) | Method for preparation of 3,3-dimethylbutyraldehyde | |
| CN102755759A (en) | Continuous reaction rectification process and rectification equipment for synthesizing isopropyl alcohol | |
| CN101830806B (en) | Method and device for co-producing dimethyl carbonate and dimethyl oxalate | |
| CN101367724B (en) | Method and apparatus for synthesis of isopropyl acetate | |
| RU2016146558A (en) | METHOD FOR PRODUCING DIMETHYL ETHER FROM GAS MIXTURES OF CARBON MONOXIDE, HYDROGEN AND METHYL ACETATE | |
| CN106631684A (en) | Method for preparing SBA(sec-butyl alcohol) through hydrolysis with sec-butyl acetate | |
| KR102224243B1 (en) | Trimethylolpropane manufacturing device and method using thereof | |
| CN104529763A (en) | Process and device for synthesizing ethyl formate with reactive distillation dividing wall column | |
| CN102452934B (en) | Preparation method of sec-butyl acetate | |
| JPH09208520A5 (en) | ||
| CN101168505B (en) | Preparation method for sec-butyl acetate with product separating and reclaiming technique | |
| CN108774100B (en) | Combined method for preparing methyl tert-butyl ether and isobutene from tert-butyl alcohol and methanol | |
| CN101130495B (en) | Method for separating sec-butyl acetate from mixture after reaction of acetic acid and butylene or mixture of C4 | |
| KR102062142B1 (en) | Method for producing Ethyl 3-Ethoxypropionate | |
| CN100443461C (en) | Method for separating sec-butyl acetate, acetic acid and heavy hydrocarbon | |
| RU2404952C1 (en) | Methyl chloride synthesis method | |
| JP4000912B2 (en) | Method for producing dimethyl carbonate | |
| CN101168506B (en) | Preparation method for sec-butyl acetate with product separating technique | |
| CN119097945B (en) | Refining device and method for nitrogen-containing solvent precursor and application | |
| CN113845426A (en) | Method and device for preparing ester compound | |
| CN110981722A (en) | Synthetic method of alcohol-containing methyl acrylate | |
| KR102224267B1 (en) | Trimethylolpropane manufacturing device and method using thereof | |
| CN101260018A (en) | Method for synthesizing exo-tetrahydrocyclopentadiene | |
| US20240092709A1 (en) | Method for producing propylene |
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 | ||
| ASS | Succession or assignment of patent right |
Owner name: HUNAN ZHONGCHUANG CHEMICAL CO., LTD. Free format text: FORMER OWNER: HU XIANNIAN Effective date: 20090731 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20090731 Address after: Yunxi District, Yueyang, Changling, Hunan Patentee after: HUNAN ZHONGCHUANG CHEMICAL CO., LTD. Address before: Hunan City, Hunan province Yunxi District Jimei village in Yueyang Chong Chemical Co., Ltd. Patentee before: Hu Xiannian |
|
| C53 | Correction of patent for invention or patent application | ||
| CB03 | Change of inventor or designer information |
Inventor after: Li Hua Inventor after: Hu Xiannian Inventor after: Liu Yudong Inventor before: Hu Xiannian Inventor before: Li Hua |
|
| COR | Change of bibliographic data |
Free format text: CORRECT: INVENTOR; FROM: HU XIANNIAN LI HUA TO: LI HUA HU XIANNIAN LIU YUDONG |