CN106397363A - Purifying method for 1,2-epoxybutane - Google Patents
Purifying method for 1,2-epoxybutane Download PDFInfo
- Publication number
- CN106397363A CN106397363A CN201510467821.0A CN201510467821A CN106397363A CN 106397363 A CN106397363 A CN 106397363A CN 201510467821 A CN201510467821 A CN 201510467821A CN 106397363 A CN106397363 A CN 106397363A
- Authority
- CN
- China
- Prior art keywords
- extractant
- epoxy butane
- distillation column
- liquid
- extraction
- 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
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D301/00—Preparation of oxiranes
- C07D301/32—Separation; Purification
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D303/00—Compounds containing three-membered rings having one oxygen atom as the only ring hetero atom
- C07D303/02—Compounds containing oxirane rings
- C07D303/04—Compounds containing oxirane rings containing only hydrogen and carbon atoms in addition to the ring oxygen atoms
Abstract
The invention relates to a purifying method for 1,2-epoxybutane. The purifying method mainly overcomes the problems of low yield of 1,2-epoxybutane, great loss of extractant and high waste water treatment cost since waste water of an extraction distillation column carries 1,2-epoxybutane and the extractant in the prior art. According to the invention, a liquid-liquid separator is additionally arranged and the extractant is used for treating and recovering 1,2-epoxybutane in waste water, so the above problems are overcome; and the purifying method provided by the invention can be applied to industrial production of purification of 1,2-epoxybutane.
Description
Technical field
The present invention relates to a kind of 1,2- epoxy butane purification process.
Background technology
1,2- epoxy butane (1,2-Butene oxide, BO), also known as butylene oxide, in manufacturing
Mesosome and polymer, for example, be used for producing 1,2- butanediol, be also used for replacing acetone as nitrate paint
Diluent.1,2- epoxy butane also can be also used for foam processed as the standard substance of chromatography
Plastics, synthetic rubber, nonionic surfactant etc..Industrial, there is the 1- of cleaning procedure
Butylene catalysis epoxidation method (as CHP method) produces 1,2- epoxy butane and is just progressively replacing traditional chlorine
Alcohol method technique.1-butylene catalysis epoxidation produce 1,2- epoxy butane during produce water, aldehyde,
The impurity such as alcohol, ester, such as methanol, water are all and 1,2- epoxy butane forms azeotropic mixture, propionic aldehyde and formic acid first
Close to 1, this results in the method using conventional distillation to the relative volatility of ester and 1,2- epoxy butane
Very difficult separating-purifying 1,2- epoxy butane.But only there is the 1,2- epoxy butane ability of higher degree
Enough polymerizations, therefore will carry out separating-purifying to 1, the 2- epoxy butane crude product of synthesis.And 1,2- epoxy
Butane occurs polymerization not require nothing more than 1,2- epoxy butane purity and reach 99.9wt%, to water impurity, aldehyde,
The content of the impurity such as alcohol and esters has strict demand.
Separate remove above impurity method generally have distillation (include extractive distillation and azeotropic distillation),
Exchange Resin by Adsorption, liquid-liquid extraction and chemical reaction handling.Chemical reaction handling mainly has
The hydrolysis of esters and the neutralization reaction (using alkali metal hydroxide) of acid, follow-up employing is distilled
Mode.The general use of chemical reaction handling is less, because some can be occurred undesirable anti-
The product loss of correlation should be caused.
Document US4402794 adopts C7-C9Hydro carbons, preferably normal octane as extractant single extract
Rectification is taken to separate the water containing in thick 1,2- epoxy butane solution, methanol, acetone, methyl formate etc. miscellaneous
Matter, is not involved with the separation of impurity aldehydes.Organic after the layering of extractive distillation column overhead phase separator
Layer removes rectifying column separated methanol, acetone etc., and tower reactor reclaims extractant, increased equipment investment
And operating cost, water layer is directly outer to be arranged, and the extractant containing in water layer and 1,2- epoxy butane lose.
Document JPS5646874 utilizes 1,2- epoxy butane to form azeotropic mixture with water, should from side take-off
Azeotropic mixture, after cooling split-phase, the organic faciess mainly containing 1,2- epoxy butane return tower, primary aqueous
Aqueous phase goes post processing.1,2- epoxy butane dissolubility in water is larger, and in aqueous phase, 1,2- epoxy butane damages
Lose larger, and increased wastewater treatment expense.
When containing aldehydes and water-solubility impurity such as alcohols (as methanol, ethanol), soluble ester (such as
Methyl formate, ethyl acetate) and during organic acid (as formic acid, acetic acid), it is also dissolved in aqueous phase
In.But a part of 1,2- epoxy butane is also dissolved in aqueous phase simultaneously.1,2- epoxy butane when 20 DEG C
Dissolve 5.91% in water, water dissolves 2.65% in 1,2- epoxy butane.Temperature is higher, dissolubility
Bigger.
During extracting rectifying, aldehyde, water, alcohol, ester impurities remove from extractive distillation column overhead
System, can carry a certain amount of 1,2- epoxy butane and extractant secretly, and direct discharge can cause 1,2- epoxy
Butane and the loss of extractant.
Content of the invention
The technical problem to be solved is folder in extractive distillation column overhead stream in prior art
With 1,2- epoxy butane and extractant, lead to that 1,2- epoxy butane yield is low, extractant loss is big
Problem, provides a kind of new 1,2- epoxy butane purification process.The method has 1,2- epoxy butane and receives
The feature that rate is high, extractant loss is low.
For solving above-mentioned technical problem, the technical scheme that the present invention takes is as follows：A kind of 1,2- epoxy fourth
Alkane purification process, comprises the following steps：
A) impure thick 1,2- epoxy butane logistics enters extraction distillation column, exists in extractant A
Lower extracting rectifying；
B) extraction distillation column tower reactor liquid phase stream enters solvent recovery tower, and tower top obtains product 1,2- ring
Oxygen butane, the extractant A that tower reactor is recycled；
C) enter phase separator after extraction distillation column top gaseous phase logistics condensation, be separated into oil reservoir and water layer；
D) optionally, described oil reservoir is recycled to extractive distillation column overhead；
E) described water layer and extractant B enter blender, enter Liquid liquid Separation device after being sufficiently mixed,
After separating, organic faciess are back to described phase separator, and aqueous phase delivers to post processing.
In technique scheme it is preferable that described thick 1,2- epoxy butane logistics be 1-butylene with organic
Obtain after peroxide reactions；Described impurity is water, C4Hydro carbons, C1～6Aldehyde, C1～6Ketone,
C1～6Alcohol, C1～6Acid or C1～6Ester at least one.
It is preferable that being calculated in mass percent in technique scheme, described thick 1,2- epoxy butane thing
In stream, the content of 1,2- epoxy butane is 92～96%, and the content of water is 2～5%, and remaining is C4Hydrocarbon
Class, C1～6Aldehyde, C1～6Ketone, C1～6Alcohol, C1～6Acid or C1～6Ester at least one.
It is preferable that described extractant A and extractant B is C in technique scheme7～C12Aliphatic series
At least one in hydrocarbon.It is highly preferred that described extractant A and extractant B is C8In aliphatic hydrocarbon
At least one.
It is preferable that the theoretical cam curve of described extraction distillation column is 30～60 in technique scheme
Block, operating pressure is 100～200kPa, and operation temperature is 60～85 DEG C, and solvent ratio is for 2～8.
It is preferable that the theoretical cam curve of described solvent recovery tower is 20～40 in technique scheme
Block, operating pressure is 100～200kPa, and operation temperature is 60～90 DEG C.
It is preferable that described Liquid liquid Separation device operating pressure is 100～300kPa in technique scheme,
Operation temperature is 30～60 DEG C.
It is preferable that the extractant A that the recovery of solvent recovery tower tower reactor obtains follows in technique scheme
Loopback extraction distillation column.
It is preferable that having one or more taper inside described Liquid liquid Separation device in technique scheme
Coalescence filter core structure.
An embodiment of the invention is：A kind of 1,2- epoxy butane purification process, walks including following
Suddenly：
A) impure thick 1,2- epoxy butane logistics enters extraction distillation column, in the presence of extractant
Extracting rectifying；
B) extraction distillation column tower reactor liquid phase stream enters solvent recovery tower, and tower top obtains product 1,2- ring
Oxygen butane, the extractant stream that tower reactor is recycled；Described extractant stream is divided into first burst of extraction
Agent logistics and second burst of extractant stream；
C) enter phase separator after extraction distillation column top gaseous phase logistics condensation, be separated into oil reservoir and water layer；
D) described first burst of extractant stream and described oil reservoir are recycled to extractive distillation column overhead；
E) described water layer and described second burst of extractant stream enter blender, enter after being sufficiently mixed
Liquid liquid Separation device, after separating, organic faciess are back to described phase separator, and aqueous phase delivers to post processing.
It is preferable that first burst of extractant stream and second burst of extractant stream in technique scheme
Weight than be (200:1)～(800:1).
In technique scheme it is preferable that described extraction distillation column top gaseous phase logistics by with
Pressure steam or deionized water contact and condense.
By, in the presence of well-known catalyst, organic peroxide and 1-butylene react
Reaction mixture to after 1,2- epoxy butane is particularly suitable, and it at least contains aldehydes as miscellaneous
Matter.In addition to containing aldehydes, also contain hydro carbons such as butylene, butane；Water；Alcohols such as methanol and
Ethanol；Organic acid；Ketone such as acetone；With esters such as methyl formate and ethyl acetate.Using with
The liquid being obtained with distillation distillation column rough segmentation before washing, then the aldehyde with separation of extractive distillation remnants,
Acid, ketone, hydro carbons, water, alcohol, ester impurities, then reclaim 1,2- epoxy butane and extraction with liquid-liquid extraction
Take agent, the loss of active component such as 1,2- epoxy butane, extractant and butylene can be reduced.
The present invention uses hydro carbons extractant first by aldehyde, acid, ketone, hydro carbons, water, alcohol, ester impurities
From thick 1,2- epoxy butane solution separation of extractive distillation out, to containing these impurity and a small amount of 1,2-
Spray into middle pressure steam or deionized water in the tower overhead gas of epoxy butane and extractant, be fully contacted and
Mixing, is separated into oil reservoir and water layer in phase separator after condensation, makes impurity enter aqueous phase as far as possible, oil
Layer and recovery extractant are recycled to extraction distillation column as extractant, also serve as flowing back simultaneously.
Water layer and the extractant reclaiming enter after blender is sufficiently mixed and enter Liquid liquid Separation device, for increasing
Plus the time of staying, improve separation efficiency in Liquid liquid Separation device for the water-oil phase, in Liquid liquid Separation device
There is one or more taper Coalescence filter core structure in portion, so that water-oil phase is repeatedly separated step by step.
With hydro carbons extractant, in Liquid liquid Separation device, the 1,2- epoxy containing in aqueous phase is reclaimed in liquid-liquid extraction
Butane is effective.After Oil-water separation in Liquid liquid Separation device, most of 1,2- epoxy butanes and extraction
Take agent to be transferred in organic faciess, and aldehyde, acid, ketone, hydro carbons, water, alcohol, ester impurities are transferred to
In aqueous phase.In addition to aldehyde, acid, ketone, hydro carbons, water, alcohol, ester impurities, a small amount of 1,2- epoxy
Butane is dissolved in the aqueous phase obtaining, in the present invention, it is preferred to pass through aqueous phase and extracting rectifying mistake
Journey identical extractant contacts, and 1, the 2- epoxy butane in aqueous phase is selectively transferred to extractant one
Side, i.e. organic faciess, thus aldehyde in 1,2- epoxy butane, acid, ketone, hydro carbons, water, alcohol,
Ester impurities are separated.By Liquid liquid Separation device, 1,2- epoxy butane is reclaimed from this organic facies, then
The loss of 1,2- epoxy butane can be reduced.Additionally, it is preferred that being steamed in extraction by recycling organic faciess
Evaporate in tower, then can reduce the loss of 1,2- epoxy butane.
Liquid liquid Separation device separation efficiency is high, equipment investment is low, do not need consumption energy consumption, can reach back
Receive the purpose of extractant and 1,2- epoxy butane.
Meanwhile, using hydro carbons as extractant during, 1 under the concurrent conditionses of water and epoxy fourth a heatable brick bed,
2- butanediol easily generates, thus 1,2- epoxy butane production or refined when inevitably generate
1,2- butanediol.1,2- butanediol exist under conditions of, extractant recycle during, meeting
Part reduces extractant effect of extracting even makes effect of extracting lose, and increases separation process energy consumption and fall
Low yield quality.Partial extraction agent is adopted to enter Liquid liquid Separation device in the present invention, 1,2- butanediol is easily
Enter aqueous phase and reach detached purpose, produce or subtractive process in 1, the 2- butanediol that produces would not be
Accumulate in system, extractant extraction efficiency can be improved.
It should be noted that the extractant disclosed in the present invention can be using one pack system it is also possible to make
Mixture with these compounds.From the viewpoint of industrial implementation, preferably industrially easily obtain
Normal heptane, normal octane.
Below by embodiment, the invention will be further elaborated.
Brief description
Fig. 1 is the process flow diagram of one embodiment of the inventive method.
In Fig. 1, T101 extraction distillation column, T102 solvent recovery tower, M101- blender,
S101 Liquid liquid Separation device, D101 phase separator.1 is thick BO charging, and 2 is extraction distillation column
T101 tower overhead gas, 3 is middle pressure steam or deionized water, and 4 is extraction distillation column T101 overhead condensation
Liquid, 5 is extraction distillation column T101 water layer, and 6 is extraction distillation column T101 organic layer, and 7 is extraction
Distillation column T101 backflow, 8 is Liquid liquid Separation device S101 extractant, and 9 is that Liquid liquid Separation device is organic
Phase, 10 is waste water (Liquid liquid Separation device aqueous phase), and 11 is extraction distillation column T101 kettle liquid, and 12 are
Solvent recovery tower T102 kettle liquid, that is, reclaim extractant, and 13 is BO product.
Using extraction distillation column T101, by thick 1, the 2- epoxy butane solution 1 containing impurity for giving
C7～C12Hydro carbons is as in the extraction distillation column of extractant；Tower overhead gas 2 in extraction distillation column T101
In spray into middle pressure steam or deionized water 3, condensed fluid 4 is separated into oil reservoir in phase separator D101
6 and water layer 5, oil reservoir 6 and reclaim extractant 12 and be recycled to extraction distillation column T101 as extractant,
Also serve as flowing back 7 simultaneously；Extraction distillation column T101 kettle liquid 11 enters solvent recovery tower T102, point
From rear, tower top obtains 1,2- epoxy butane product 13, and solvent recovery tower bottoms 12 is divided into two strands, its
In one I is recycled to extraction distillation column as extractant, in addition one II delivers to blender M101
Liquid liquid Separation device S101 is entered, after separating, organic faciess 9 are back to split-phase after being sufficiently mixed with logistics 5
Device, aqueous phase 10 delivers to post processing.
Below by embodiment, the invention will be further elaborated.
Specific embodiment
【Embodiment 1】
Thick 1,2- epoxy butane solution is calculated in mass percent, 1,2- epoxy butane 93.5%, water 5%,
Remaining is propionic aldehyde, methanol and methyl formate impurity.
Using extraction distillation column T101, by thick 1, the 2- epoxy butane solution 1 containing impurity for giving
C7～C12Hydro carbons is as in the extractive distillation of extractant；In the tower overhead gas 2 of extraction distillation column T101
Spray into middle pressure steam or deionized water 3, condensed fluid 4 is separated into oil reservoir 6 in phase separator D101
With water layer 5, oil reservoir 6 and reclaim extractant 12 and be recycled to extraction distillation column T101 as extractant,
Also serve as flowing back 7 simultaneously；Extraction distillation column T101 kettle liquid 11 enters solvent recovery tower T102, point
From rear, tower top obtains 1,2- epoxy butane product 13, and solvent recovery tower bottoms 12 is divided into two strands, its
In one I is recycled to extraction distillation column as extractant, in addition one II delivers to blender M101
Liquid liquid Separation device S101 is entered, after separating, organic faciess 9 are back to split-phase after being sufficiently mixed with logistics 5
Device, aqueous phase 10 delivers to post processing.
Wherein, the theoretical cam curve of extraction distillation column is 35 pieces, and operating pressure is 120kPa, operation
Temperature is 67 DEG C.
The solvent of extraction distillation column is than for 6.
The theoretical cam curve of solvent recovery tower is 25 pieces, and operating pressure is 120kPa, and operation temperature is
69℃.
Liquid liquid Separation device operating pressure is 110kPa, and operation temperature is 45 DEG C.
Extractant A is normal octane.
The weight of logistics I and logistics II is than for 500：1.
It is calculated in mass percent, in logistics 13,1,2- epoxy butane product purity reaches 99.95%, third
Aldehyde 15ppm, normal octane 15ppm., more than 99%, extractant loss is little for 1, the 2- epoxy butane response rate
In 0.02%.
【Embodiment 2】
Thick 1,2- epoxy butane solution is calculated in mass percent, 1,2- epoxy butane 94.5%, water 4%,
Remaining is propionic aldehyde, methanol and methyl formate impurity.
Embodiment with【Embodiment 1】Identical, except for the difference that：
The theoretical cam curve of extraction distillation column is 45 pieces, and operating pressure is 160kPa, and operation temperature is
78℃.
The solvent of extraction distillation column is than for 5.
The theoretical cam curve of solvent recovery tower is 35 pieces, and operating pressure is 160kPa, operation temperature
For 80 DEG C.
Liquid liquid Separation device operating pressure is 130kPa, and operation temperature is 40 DEG C.
Extractant A is isobutyltrimethylmethane..
The weight of logistics I and logistics II is than for 600：1.
It is calculated in mass percent, in logistics 13,1,2- epoxy butane product purity reaches 99.96%, third
Aldehyde 10ppm, normal octane 10ppm.More than 99.2%, extractant loses 1, the 2- epoxy butane response rate
Less than 0.025%.
【Embodiment 3】
Thick 1,2- epoxy butane solution is calculated in mass percent, 1,2- epoxy butane 96%, water 2%,
Remaining is propionic aldehyde, methanol and methyl formate impurity.
Embodiment with【Embodiment 1】Identical, except for the difference that：
The theoretical cam curve of extraction distillation column is 60 pieces, and operating pressure is 200kPa, and operation temperature is
85℃.
The solvent of extraction distillation column is than for 4.
The theoretical cam curve of solvent recovery tower is 40 pieces, and operating pressure is 200kPa, operation temperature
For 90 DEG C.
Liquid liquid Separation device operating pressure is 160kPa, and operation temperature is 45 DEG C.
Extractant A is 2- methylpentane.
The weight of logistics I and logistics II is than for 650：1.
It is calculated in mass percent, in logistics 13,1,2- epoxy butane product purity reaches 99.98%, third
Aldehyde 5ppm, normal octane 8ppm., more than 99.4%, extractant loss is little for 1, the 2- epoxy butane response rate
In 0.01%.
【Comparative example 1】
Embodiment with【Embodiment 1】Identical, except for the difference that cancel Liquid liquid Separation device.
It is calculated in mass percent, in logistics 13,1,2- epoxy butane product purity reaches 99.95%, third
Aldehyde 50ppm, normal octane 50ppm.1, the 2- epoxy butane response rate is 95%, and extractant loss is more than
1%.
【Comparative example 2】
Embodiment with【Embodiment 1】Identical, Liquid liquid Separation device washes tower (liquid-liquid extraction tower) with water.
It is calculated in mass percent, in logistics 13,1,2- epoxy butane product purity reaches 99.95%, third
Aldehyde 50ppm, normal octane 50ppm.1, the 2- epoxy butane response rate is 98%, and extractant loss is more than
0.05%.
Closed from the above it can be seen that implementing the present invention and being separated with economic and convenient method
1, the 2- epoxy butane product of lattice, improves product yield, reduces extractant loss.
Claims (10)
1. one kind 1,2- epoxy butane purification process, comprise the following steps：
A) impure thick 1,2- epoxy butane logistics enters extraction distillation column, exists in extractant A
Lower extracting rectifying；
B) extraction distillation column tower reactor liquid phase stream enters solvent recovery tower, and tower top obtains product 1,2- ring
Oxygen butane, the extractant A that tower reactor is recycled；
C) enter phase separator after extraction distillation column top gaseous phase logistics condensation, be separated into oil reservoir and water layer；
D) optionally, described oil reservoir is recycled to extractive distillation column overhead；
E) described water layer and extractant B enter blender, enter Liquid liquid Separation device after being sufficiently mixed,
After separating, organic faciess are back to described phase separator, and aqueous phase delivers to post processing.
2. according to claim 11,2- epoxy butane purification process it is characterised in that described
Thick 1,2- epoxy butane logistics is obtained after being reacted with organic peroxide for 1-butylene；Described impurity
For water, C4Hydro carbons, C1～6Aldehyde, C1～6Ketone, C1～6Alcohol, C1～6Acid or C1～6Ester in
At least one.
3. according to claim 21,2- epoxy butane purification process it is characterised in that with quality
Percent meter, in described thick 1,2- epoxy butane logistics, the content of 1,2- epoxy butane is 92～96%,
The content of water is 2～5%, and remaining is C4Hydro carbons, C1～6Aldehyde, C1～6Ketone, C1～6Alcohol, C1～6
Acid or C1～6Ester at least one.
4. according to claim 11,2- epoxy butane purification process it is characterised in that described extraction
Agent A and extractant B is taken to be C7～C12At least one in aliphatic hydrocarbon.
5. according to claim 41,2- epoxy butane purification process it is characterised in that described extraction
Agent A and extractant B is taken to be C8At least one in aliphatic hydrocarbon.
6. according to claim 11,2- epoxy butane purification process it is characterised in that described extraction
The theoretical cam curve taking distillation column is 30～60 pieces, and operating pressure is 100～200kPa, operation temperature
For 60～85 DEG C, solvent is than for 2～8；
The theoretical cam curve of described solvent recovery tower is 20～40 pieces, and operating pressure is 100～200kPa,
Operation temperature is 60～90 DEG C；
Described Liquid liquid Separation device operating pressure is 100～300kPa, and operation temperature is 30～60 DEG C.
7. according to claim 11,2- epoxy butane purification process it is characterised in that solvent returns
Receipts tower tower reactor reclaims the extractant A obtaining and loops back extraction distillation column.
8. according to claim 11,2- epoxy butane purification process it is characterised in that described liquid
There is one or more taper Coalescence filter core structure inside liquid/gas separator.
9. one kind 1,2- epoxy butane purification process, comprise the following steps：
A) impure thick 1,2- epoxy butane logistics enters extraction distillation column, in the presence of extractant
Extracting rectifying；
B) extraction distillation column tower reactor liquid phase stream enters solvent recovery tower, and tower top obtains product 1,2- ring
Oxygen butane, the extractant stream that tower reactor is recycled；Described extractant stream is divided into first burst of extraction
Agent logistics and second burst of extractant stream；
C) enter phase separator after extraction distillation column top gaseous phase logistics condensation, be separated into oil reservoir and water layer；
D) described first burst of extractant stream and described oil reservoir are recycled to extractive distillation column overhead；
E) described water layer and described second burst of extractant stream enter blender, enter after being sufficiently mixed
Liquid liquid Separation device, after separating, organic faciess are back to described phase separator, and aqueous phase delivers to post processing.
10. according to claim 91,2- epoxy butane purification process it is characterised in that first strand
The weight ratio of extractant stream and second burst of extractant stream is (200:1)～(800:1)；Described extraction is steamed
Evaporate column overhead gaseous stream by contacting and condensing with middle pressure steam or deionized water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510467821.0A CN106397363B (en) | 2015-08-03 | 2015-08-03 | 1,2- epoxy butane purification process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510467821.0A CN106397363B (en) | 2015-08-03 | 2015-08-03 | 1,2- epoxy butane purification process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106397363A true CN106397363A (en) | 2017-02-15 |
| CN106397363B CN106397363B (en) | 2019-08-06 |
Family
ID=58007882
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510467821.0A Active CN106397363B (en) | 2015-08-03 | 2015-08-03 | 1,2- epoxy butane purification process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106397363B (en) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108017598A (en) * | 2016-11-04 | 2018-05-11 | 中国石油化工股份有限公司 | Epoxy butane composition and preparation method thereof |
| CN108017597A (en) * | 2016-11-04 | 2018-05-11 | 中国石油化工股份有限公司 | Epoxy butane composition |
| CN109851591A (en) * | 2018-02-22 | 2019-06-07 | 中国石油化工股份有限公司 | The purification process and device of epoxyalkane |
| CN109851579A (en) * | 2017-11-30 | 2019-06-07 | 中国石油化工股份有限公司 | Epoxyalkane production method |
| CN109851584A (en) * | 2017-11-30 | 2019-06-07 | 中国石油化工股份有限公司 | The refining methd and device of epoxyalkane |
| CN109851576A (en) * | 2017-11-30 | 2019-06-07 | 中国石油化工股份有限公司 | Epoxy butane purification process and purification devices |
| CN109851585A (en) * | 2017-11-30 | 2019-06-07 | 中国石油化工股份有限公司 | The purification process of epoxy butane |
| CN110357838A (en) * | 2019-07-16 | 2019-10-22 | 湖南理工学院 | Fractional extraction separating-purifying 1,2- epoxy butane new method |
| CN112694456A (en) * | 2019-10-23 | 2021-04-23 | 中国石油化工股份有限公司 | Method for pretreating and supplementing extracting agent in propylene oxide purification process |
| CN112851601A (en) * | 2019-11-27 | 2021-05-28 | 北京诺维新材科技有限公司 | Method for purifying alkylene oxide |
| CN113651778A (en) * | 2020-05-12 | 2021-11-16 | 中国石油化工股份有限公司 | Extraction agent pretreatment and supplement method |
| CN115845484A (en) * | 2023-02-21 | 2023-03-28 | 中国科学院过程工程研究所 | Separation and refining device and method for crude epoxybutane product |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4402794A (en) * | 1982-05-24 | 1983-09-06 | Atlantic Richfield Company | Purification of butylene oxides by extractive distillation with selected extractive distillation solvents |
| CN104109137A (en) * | 2013-04-16 | 2014-10-22 | 中国石油化工股份有限公司 | Epoxypropane purifying method |
-
2015
- 2015-08-03 CN CN201510467821.0A patent/CN106397363B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4402794A (en) * | 1982-05-24 | 1983-09-06 | Atlantic Richfield Company | Purification of butylene oxides by extractive distillation with selected extractive distillation solvents |
| CN104109137A (en) * | 2013-04-16 | 2014-10-22 | 中国石油化工股份有限公司 | Epoxypropane purifying method |
Non-Patent Citations (1)
| Title |
|---|
| 胡松等: "萃取精馏分离环氧丙烷-水-甲醇化合物的模拟", 《石油化工》 * |
Cited By (24)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108017598A (en) * | 2016-11-04 | 2018-05-11 | 中国石油化工股份有限公司 | Epoxy butane composition and preparation method thereof |
| CN108017597A (en) * | 2016-11-04 | 2018-05-11 | 中国石油化工股份有限公司 | Epoxy butane composition |
| CN108017598B (en) * | 2016-11-04 | 2021-06-22 | 中国石油化工股份有限公司 | Epoxy butane composition and preparation method thereof |
| CN108017597B (en) * | 2016-11-04 | 2021-06-22 | 中国石油化工股份有限公司 | Epoxy butane composition |
| CN109851585A (en) * | 2017-11-30 | 2019-06-07 | 中国石油化工股份有限公司 | The purification process of epoxy butane |
| CN109851576B (en) * | 2017-11-30 | 2021-05-11 | 中国石油化工股份有限公司 | Method and apparatus for purifying butylene oxide |
| CN109851584A (en) * | 2017-11-30 | 2019-06-07 | 中国石油化工股份有限公司 | The refining methd and device of epoxyalkane |
| CN109851583A (en) * | 2017-11-30 | 2019-06-07 | 中国石油化工股份有限公司 | Epoxyalkane purification process |
| CN109851579A (en) * | 2017-11-30 | 2019-06-07 | 中国石油化工股份有限公司 | Epoxyalkane production method |
| CN109851585B (en) * | 2017-11-30 | 2021-02-09 | 中国石油化工股份有限公司 | Method for purifying butylene oxide |
| CN109851579B (en) * | 2017-11-30 | 2021-02-09 | 中国石油化工股份有限公司 | Process for producing alkylene oxide |
| CN109851583B (en) * | 2017-11-30 | 2021-03-30 | 中国石油化工股份有限公司 | Alkylene oxide purification process |
| CN109851584B (en) * | 2017-11-30 | 2021-05-11 | 中国石油化工股份有限公司 | Method and apparatus for purifying alkylene oxide |
| CN109851576A (en) * | 2017-11-30 | 2019-06-07 | 中国石油化工股份有限公司 | Epoxy butane purification process and purification devices |
| CN109851591B (en) * | 2018-02-22 | 2021-05-11 | 中国石油化工股份有限公司 | Method and apparatus for purifying alkylene oxide |
| CN109851591A (en) * | 2018-02-22 | 2019-06-07 | 中国石油化工股份有限公司 | The purification process and device of epoxyalkane |
| CN110357838A (en) * | 2019-07-16 | 2019-10-22 | 湖南理工学院 | Fractional extraction separating-purifying 1,2- epoxy butane new method |
| CN112694456A (en) * | 2019-10-23 | 2021-04-23 | 中国石油化工股份有限公司 | Method for pretreating and supplementing extracting agent in propylene oxide purification process |
| CN112694456B (en) * | 2019-10-23 | 2023-09-29 | 中国石油化工股份有限公司 | Method for pretreating and supplementing extractant in epoxypropane purification process |
| CN112851601A (en) * | 2019-11-27 | 2021-05-28 | 北京诺维新材科技有限公司 | Method for purifying alkylene oxide |
| CN113651778A (en) * | 2020-05-12 | 2021-11-16 | 中国石油化工股份有限公司 | Extraction agent pretreatment and supplement method |
| CN113651778B (en) * | 2020-05-12 | 2023-06-06 | 中国石油化工股份有限公司 | Extraction agent pretreatment and replenishment method |
| CN115845484A (en) * | 2023-02-21 | 2023-03-28 | 中国科学院过程工程研究所 | Separation and refining device and method for crude epoxybutane product |
| CN115845484B (en) * | 2023-02-21 | 2023-04-28 | 中国科学院过程工程研究所 | Separation and refining device and method for crude product of epoxybutane |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106397363B (en) | 2019-08-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106397363A (en) | Purifying method for 1,2-epoxybutane | |
| TWI500608B (en) | Purification of propylene oxide | |
| CN109851586B (en) | Process for purifying propylene oxide | |
| CN106397361B (en) | The method for purifying 1,2- epoxy butane | |
| CN105980338B (en) | By the method for the raw material production 1,3-butadiene comprising ethyl alcohol | |
| CN107286119B (en) | Method for purifying propylene oxide | |
| CN108002995B (en) | Method and equipment for synthesizing methyl isobutyl ketone by acetone two-step method | |
| CN106397365B (en) | 1,2- epoxy butane purification devices | |
| CN104447198B (en) | Separation technology for preparation of isopropanol by acetone hydrogenation | |
| CN106397366B (en) | The purification process of propylene oxide | |
| CN104109138A (en) | Epoxypropane purifying method | |
| WO2006001407A1 (en) | Method of purifying propylene oxide | |
| CN106397364B (en) | The purification devices of propylene oxide | |
| CN102161008B (en) | Method for recovering catalyst in preparation of cyclohexene by partial hydrogenation of benzene | |
| RU2408569C2 (en) | Method of producing allyl alcohol | |
| CN105085165B (en) | The separation method of ethylene glycol and diethylene glycol | |
| US10463987B2 (en) | Process for purifying an aqueous solution comprising diethylacetal | |
| CN109851589A (en) | Oxide purification process and purification devices | |
| CN112851601B (en) | Method for purifying alkylene oxide | |
| CN107286118A (en) | The refining plant of expoxy propane | |
| CN112209903B (en) | Purification method of propylene oxide | |
| CN109851577B (en) | Method for purifying butylene oxide | |
| CN107915615A (en) | The method that the MIBK of purification is prepared by industrial by-product waste liquid acetone | |
| EP2785672B1 (en) | Caustic treatment of formaldehyde recycle column feed | |
| CN112079688A (en) | Method and device for separating and refining coal and biomass-based ethylene glycol liquid-phase product |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |