CN109851587A - The production method of epoxy butane - Google Patents
The production method of epoxy butane Download PDFInfo
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- CN109851587A CN109851587A CN201711241136.1A CN201711241136A CN109851587A CN 109851587 A CN109851587 A CN 109851587A CN 201711241136 A CN201711241136 A CN 201711241136A CN 109851587 A CN109851587 A CN 109851587A
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- epoxy butane
- extractant
- glycol
- knockout tower
- azeotropic mixture
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Abstract
The present invention relates to a kind of production methods of epoxy butane, mainly solve the problems, such as that glycol heavy constituent impurities accumulation leads to that extractant purity is low, loss is big, epoxy butane yield is low, energy consumption is high in the prior art.The method includes the logistics containing epoxy butane, extractant and glycol the step of knockout tower separates；The knockout tower operates under conditions of being enough makes extractant and glycol formation azeotropic mixture, and, in logistics of the knockout tower side take-off containing extractant and glycol azeotropic mixture.The method can be used in the industrial production of epoxy butane.
Description
Technical field
The present invention relates to a kind of production methods of epoxy butane, and in particular to epoxy butane extracting rectifying recycles extractant
Purification process.
Background technique
1,2- epoxy butane (BO) same to ethylene oxide (EO) and propylene oxide (PO) belong to homologue, molecular formula C4H8O(CAS
Number: be a kind of substance with three-membered ring structures 106-88-7), chemical property is active, be mainly used as polyether polyols alcohol monomer and
The intermediate of other synthetic materials.It is living that 1,2- epoxy butane can be also used for foamed plastics processed, synthetic rubber, non-ionic surface
Property agent etc., can also replace diluent of the acetone as nitrate paint, it is also possible to make the standard substance of chromatography.
As olefin epoxide, compared with ethylene oxide and propylene oxide, on molecular structure, epoxy butane possesses more
- the CH of multi-quantity2Functional group, when as monomer synthesizing polyether glycol, product has excellent hydrophobic performance, especially
Suitable for certain outer surface waterproof coatings for requiring stringent building and equipment.Meanwhile institute is copolymerized by monomer of epoxy butane
The polyurethane material of synthesis possesses excellent cold tolerance, especially suitable for weather severe cold area.
Epoxy butane product has strict demand to water, aldehyde, isomer, and water will affect the hydroxyl value and foaminess of polymer
Can, the content of aldehyde is environmental requirement, and isomer is the end-capping reagent for polymerizeing long-chain, therefore, to production in national standard and company standard
Product purity has strict demand.
1,2- epoxy butane qualified product quality purity requirement in BASF company standard are as follows: epoxy butane >=99.5%, epoxy
Butane isomer≤0.2%, total aldehyde≤0.05%, water≤0.03%.
1,2- epoxy butane high-class product quality purity requirement are as follows: epoxy butane >=99.9%, epoxy butane isomer
≤ 0.1%, total aldehyde≤0.015%, water≤0.005%.
It reacts in the thick epoxy butane generated and usually contains the impurity such as water, methanol, acetone, methyl formate, because these are miscellaneous
Matter and epoxy butane form azeotropic mixture or relative volatility close to 1, and conventional distillation is difficult to reach epoxy butane product standard.For
It obtains meeting the high-purity epoxy butane that polymerization requires, it is necessary to be separated off the impurity contained in epoxy butane.
The purifying of epoxy butane generally uses C7~C20 straight chain and branch hydro carbons and (or) glycols as extractant.From
Economy considers that the purification process of epoxy butane is using the mixture of C8 straight chain and branched paraffin as extractant.Extractant
Addition makes acetaldehyde, water, methanol, methyl formate become larger epoxy butane relative volatility, and acetaldehyde, water, methanol, methyl formate are from tower
Top removes.
In butylene epoxidation reaction product, mainly 1,2- epoxy butane and its isomer such as Isosorbide-5-Nitrae-epoxy butane,
2,3- epoxy butanes, epoxy iso-butane, in epoxy butane subtractive process, due to the presence of water, inevitably, 1,2- epoxy fourth
Alkane and its isomerism know from experience hydrolysis and generate 1,2- butanediol and corresponding glycol, and with time hydrolysis continue into
Row.If glycol is not separated off in extractant, it will lasting accumulation causes glycol content in cycling extraction agent excessively high, extracts
Taking the effect of extracting of agent can decline until losing effect of extracting.But glycol is dissolved in water mostly, while also being soluble in epoxy butane etc.
Organic solvent, method removal efficiency during Phase separation through washing is low, while also aggravating the hydrolysis of epoxy butane.And
And since the boiling point of glycol is higher than extractant C8 hydro carbons, so tiring out simultaneously when extractant being recycled in system with extractant
Product circulation, to reduce the effect of extracting of extractant.So reducing the concentration of glycol in extractant is very important.Example
Such as, document US4402794 discloses the hydro carbons using C7-C9, preferably normal octane as extractant single separation of extractive distillation thick 1,
The impurity such as water, methanol, acetone, the methyl formate contained in 2- epoxy butane solution.After the layering of extractive distillation column overhead phase-splitter
Organic layer remove rectifying column distillation separation methanol, acetone etc.；Extractive distillation column is sent into extraction distillation column tower reactor logistics；Extracting rectifying
Tower tower bottoms part outlet.This method contains extractant and 1 by outlet part, and the tower bottoms of 2- butanediol is being extracted with reducing it
Take the accumulation in agent.Since 1, the 2- butanediol content in tower reactor outlet fraction of stream is low, to guarantee extractant purity, it is necessary to
The a large amount of extractant of outlet, thus larger amount of extractant can be lost.
Document US4772732 discloses a kind of by using anion exchange resin and adsorbent purifying butene oxide
Method.Anion exchange resin removes acid and dehydrogenation impurity, and adsorbent removes the water of the impurity from epoxy butane.According to miscellaneous
Matter content, purification step can carry out alone or in combination, and the process can be conducted batch-wise in the reactor, or in tower or
It is carried out continuously in column.Selected ion exchange resin is the big netted anion exchange resin of sulfonation, and adsorbent is molecular sieve.
This method higher cost, absorption resolving also can be cumbersome, and treating capacity is little.
The current status of the prior art is that a kind of small, with high purity, the epoxy butane high income of extractant loss is still required,
The small epoxy butane production method of energy consumption.
Summary of the invention
The present inventor passes through diligent the study found that miscellaneous using extractant and glycol heavy constituent on the basis of existing technology
Matter forms azeotropic mixture, from knockout tower side take-off azeotropic mixture, so that it may solve the problems, such as that at least one is aforementioned, and this completes
The present invention.
Specifically, the present invention relates to a kind of production methods of epoxy butane.The method includes containing epoxy butane, extraction
Agent and the logistics of glycol are the step of knockout tower separates；
The knockout tower operates under conditions of being enough makes extractant and glycol formation azeotropic mixture, and
In logistics of the knockout tower side take-off containing extractant and glycol azeotropic mixture.
According to an aspect of the present invention, described to be enough that extractant and glycol is made to form the condition of azeotropic mixture to include: pressure
0.02~0.40MPaA, preferably 0.10~0.20MPaA；80~180 DEG C of azeotropic mixture temperature, preferably 120~150 DEG C.
According to an aspect of the present invention, the knockout tower number of theoretical plate be 15~80, preferably 20~65, more preferable 20~
50。
According to an aspect of the present invention, the position of azeotropic mixture described in knockout tower side take-off is located at knockout tower tower bottom and boils again
1st~8 piece of theoretical plate on device return port, preferably the 2nd~6 piece of theoretical plate, more preferable 2nd~4 piece of theoretical plate.
According to an aspect of the present invention, in the logistics containing epoxy butane, extractant and glycol, with weight percent
The ratio of meter, extractant and epoxy butane is (2~25): 1, preferably (3~20): 1, more preferable (5~13): 1.
According to an aspect of the present invention, the logistics containing epoxy butane, extractant and glycol is originated from alkene epoxidation
The extraction product stream that reaction product obtains after extracting rectifying.
According to an aspect of the present invention, the glycol includes epoxy butane and/or the hydrolysate of its isomer.
Beneficial effects of the present invention: the method for the present invention forms azeotropic mixture using extractant and glycol heavy constituent impurity, from point
From tower side take-off azeotropic mixture, thus glycol heavy constituent impurity is discharged from extractant circulating system, decontamination cycle extractant,
Extractant purity is improved, reduces the loss and energy consumption of extractant, improves the yield of epoxy butane.It is direct with the prior art
The scheme of knockout tower tower reactor stream portions outlet to be compared, extractant purity improves 0.1~2%, extractant loss 0.1~
1.3%, energy consumption reduces 1~10%, and epoxy butane yield improves 0.5~5%.
Detailed description of the invention
Fig. 1 is the flow diagram of the method for the invention.
Fig. 2 is the flow diagram of existing technical literature US4402794 the method.
In the accompanying drawings, identical component uses identical appended drawing reference.Attached drawing is not according to actual ratio.
Description of symbols:
1 feed stream
2 extractant streams
3 epoxy butane product streams
4 reboiler feed streams
5 reboiler output streams
6 logistics containing extractant and glycol azeotropic mixture
A knockout tower
B reboiler
The present invention is described in detail with reference to the accompanying drawing, it should be noted however that protection scope of the present invention is simultaneously
It is not limited, it but is determined by the appended claims.
All publications, patent application, patent and the other bibliography that this specification is mentioned all are incorporated by reference into
Herein.Unless otherwise defined, all technical and scientific terms used herein all there are those skilled in the art routinely to manage
The meaning of solution.In case of conflict, it is subject to the definition of this specification.
When this specification with prefix " well known to those skilled in the art ", " prior art " or its export material similar to term
Whens material, substance, method, step, device or component etc., object derived from the prefix is covered this field when the application proposes and is routinely made
Those of with, but also include also being of little use at present, it will but become art-recognized for suitable for those of similar purpose.
In the context of the present specification, other than the content clearly stated, any matters or item that do not mention are equal
It is directly applicable in those of known in the art without carrying out any change.Moreover, any embodiment described herein can be with
It is freely combined with one or more other embodiments described herein, the technical solution or technical idea formed therefrom regards
For the original disclosure of the present invention or a part of original description, and be not considered as not disclosing or be expected herein it is new in
Hold, unless those skilled in the art think that the combination is obvious unreasonable.
In the case where not clearly indicating, all percentages, number, the ratio etc. being previously mentioned in this specification be all with
On the basis of weight, unless not meeting the conventional understanding of those skilled in the art when using weight as benchmark.
In the case where not clearly indicating, all pressure being previously mentioned in this specification are all absolute pressures.
Raw material used in the method for the present invention is the logistics containing epoxy butane and extractant.It is anti-that the logistics is originated from alkene epoxidation
The extraction product stream for answering product to obtain after extractive distillation column (attached drawing of the present invention is not directed to) extracting rectifying.In the method for the present invention
To purified extractant can return extractive distillation column be recycled.
The extractant that epoxy butane purifying uses is known.Generally using C7~C20 straight chain and branch hydro carbons and
(or) glycols is as extractant.From economic considerations, using the mixture of C8 straight chain and branched paraffin as extractant, such as
Normal octane, isooctane, 2- methyl-heptan.From extractant cost consideration is reduced, mixture is preferably selected.
According to the present invention, in Fig. 1, the logistics 1 containing epoxy butane, extractant and glycol enters knockout tower A, and epoxy butane produces
Product logistics 3 is removed from separation column, and extractant stream 2 is removed from separation tower bottom, and the extractant of removal can return to preamble
Extractive distillation column (being not drawn into attached drawing) be recycled.The bottom knockout tower A is equipped with reboiler B, and reboiler B feed stream 4 will
Reboiler B output streams 5 are obtained after tower bottoms feeding reboiler B heating and send the lower part knockout tower A back to, contain extractant and glycol azeotropic
The logistics 6 of object is from knockout tower A side take-off, and thus glycol is discharged from system.
According to the present invention, the position of knockout tower side take-off selection glycol enrichment, the position of the azeotropic mixture are located at separation
1st~8 piece of theoretical plate on tower tower bottom reboiler return port, preferably the 2nd~6 piece of theoretical plate, more preferable 2nd~4 piece of theoretical plate.
In this position, glycol content highest in azeotropic mixture composition, the epoxy butane amount taken out of is minimum.More up, in azeotropic mixture composition
Epoxy butane concentration is higher, and diol concentration is lower, and the epoxy butane taken out of when producing azeotropic mixture is more, loses bigger.
According to the present invention, the condition for being enough to make extractant and glycol to form azeotropic mixture include: pressure 0.02~
0.40MPaA considers that tower top epoxy butane gas phase uses cooling water as cooling medium, in the case where meeting operating pressure, to the greatest extent
Amount reduces operating pressure to reduce equipment material requirement, preferably 0.10~0.20MPaA, and 80~180 DEG C of azeotropic mixture temperature, preferably
120~150 DEG C.
By taking 1,2- butanediol as an example, with pressure rise, glycol content increases in azeotropic mixture, and pressure 0.06MPaA is corresponding
3.63wt%, pressure 0.10MPaA correspond to 4.90wt%, and pressure 0.15MPaA corresponds to 6.16wt%, and pressure 0.20MPaA is corresponding
7.21wt%.Glycol content is higher in azeotropic mixture, and in the identical situation of side take-off amount, the glycol of extraction is more, corresponding extraction
Take agent loss fewer.But since tower top is epoxy butane, epoxy butane temperature is more than 120 DEG C, it may occur that the side reactions such as polymerization, drop
Low epoxy butane yield, while bottom temperature is higher higher to steam class requirement, comprehensively considers preferably 0.10~0.20MPaA,
Corresponding 120~150 DEG C of azeotropic mixture temperature.
It should be noted that the concentration about glycol in the logistics containing epoxy butane, extractant and glycol, due to refining
Under the conditions of having existing for water, 1,2- epoxy butane and its isomerism are known from experience not for Cheng Zhong, epoxy butane and its isomer
Generation 1,2- butanediol and corresponding glycol are hydrolyzed disconnectedly, so its concentration can continue with the lasting progress of hydrolysis
Increase.
Fig. 2 is the prior art, and the logistics 1 containing epoxy butane, extractant and glycol enters knockout tower A, epoxy butane product
Logistics 3 removes at the top of knockout tower A, and extractant stream 2 is removed from separation tower bottom, and the bottom knockout tower A is equipped with reboiler B, then
Tower bottoms is sent into after reboiler B heating by boiling device B feed stream 4 obtains the feeding of reboiler B output streams 5 lower part knockout tower C, extraction
It takes agent logistics 2 to separate one logistics 6, takes this glycol system is discharged.Due to passing through the tower reactor logistics of outlet part to reduce glycol
Accumulation in extractant, thus larger amount of extractant can be lost.
Below by specific embodiment, the invention will be further elaborated.
Specific embodiment
[embodiment 1]
According to process flow shown in Fig. 1, extractant is normal octane, contains the logistics of 1,2- epoxy butane, extractant and glycol
In, by weight percentage, extractant and 1, the ratio of 2- epoxy butane is 12:1, knockout tower number of theoretical plate 30, knockout tower side
Line extraction is located at the 2nd piece of theoretical plate on reboiler return port.Knockout tower operating pressure 0.10MPaA, temperature are 68 DEG C, side line
129 DEG C of azeotropic mixture azeotropic temperature, glycol content 5.44wt% of extraction, the enrichment extraction of side line glycol.
It is 99.95% that separation column, which obtains 1,2- epoxy butane product purity, and the rate of recovery 99.81% separates tower bottom
Extractant purity 98.45%, extractant loss 0.85%.
[embodiment 2]
According to process flow chart shown in Fig. 1, extractant is normal octane, the object containing 1,2- epoxy butane, extractant and glycol
In stream, by weight percentage, extractant and 1, the ratio of 2- epoxy butane is 11:1, knockout tower number of theoretical plate 30, knockout tower
Side take-off is located at the 2nd piece of theoretical plate on reboiler return port.Knockout tower operating pressure 0.10MPaA, temperature are 68 DEG C, side
Line produces 129 DEG C of azeotropic mixture azeotropic temperature, glycol content 5.44wt%, the enrichment extraction of side line glycol.
It is 99.95% that separation column, which obtains 1,2- epoxy butane product purity, and the rate of recovery 99.83% separates tower bottom
Extractant purity 98.51%, extractant loss 0.90%.
[embodiment 3]
According to process flow chart shown in Fig. 1, extractant is normal octane, the object containing 1,2- epoxy butane, extractant and glycol
In stream, by weight percentage, extractant and 1, the ratio of 2- epoxy butane is 10:1, knockout tower number of theoretical plate 30, knockout tower
Side take-off is located at the 2nd piece of theoretical plate on reboiler return port.Knockout tower operating pressure 0.10MPaA, temperature are 68 DEG C, side
Line produces 129 DEG C of azeotropic mixture azeotropic temperature, glycol content 5.44wt%, the enrichment extraction of side line glycol.
It is 99.94% that separation column, which obtains 1,2- epoxy butane product purity, and the rate of recovery 99.84% separates tower bottom
Extractant purity 98.55%, extractant loss 0.93%.
[embodiment 4]
According to process flow chart shown in Fig. 1, extractant is normal octane, the object containing 1,2- epoxy butane, extractant and glycol
In stream, by weight percentage, extractant and 1, the ratio of 2- epoxy butane is 8:1, knockout tower number of theoretical plate 30, knockout tower side
Line extraction is located at the 2nd piece of theoretical plate on reboiler return port.Knockout tower operating pressure 0.10MPaA, temperature are 68 DEG C, side line
129 DEG C of azeotropic mixture azeotropic temperature, glycol content 5.44wt% of extraction, the enrichment extraction of side line glycol.
It is 99.95% that separation column, which obtains 1,2- epoxy butane product purity, and the rate of recovery 99.88% separates tower bottom
Extractant purity 98.23%, extractant loss 0.94%.
[embodiment 5]
According to process flow chart shown in Fig. 1, extractant is normal octane, the object containing 1,2- epoxy butane, extractant and glycol
In stream, by weight percentage, extractant and 1, the ratio of 2- epoxy butane is 6:1, knockout tower number of theoretical plate 30, knockout tower side
Line extraction is located at the 2nd piece of theoretical plate on reboiler return port.Knockout tower operating pressure 0.10MPaA, temperature are 68 DEG C, side line
129 DEG C of azeotropic mixture azeotropic temperature, glycol content 5.44wt% of extraction, the enrichment extraction of side line glycol.
It is 99.95% that separation column, which obtains 1,2- epoxy butane product purity, and the rate of recovery 99.87% separates tower bottom
Extractant purity 98.02%, extractant loss 0.97%.
[embodiment 6]
According to process flow chart shown in Fig. 1, extractant is C8 saturated alkane mixture, contains 1,2- epoxy butane, extractant
In the logistics of glycol, by weight percentage, extractant and 1, the ratio of 2- epoxy butane is 6:1, knockout tower number of theoretical plate
30, knockout tower side take-off is located at the 2nd piece of theoretical plate on reboiler return port.Knockout tower operating pressure 0.10MPaA, temperature
It is 68 DEG C, 125 DEG C, glycol content 5.01wt% of side take-off azeotropic mixture azeotropic temperature, the enrichment extraction of side line glycol.
It is 99.95% that separation column, which obtains 1,2- epoxy butane product purity, and the rate of recovery 99.84% separates tower bottom
Extractant purity 98.05%, extractant loss 1.00%.
[embodiment 7]
According to process flow chart shown in Fig. 1, extractant is normal octane, the object containing 1,2- epoxy butane, extractant and glycol
In stream, by weight percentage, extractant and 1, the ratio of 2- epoxy butane is 10:1, knockout tower number of theoretical plate 15, knockout tower
Side take-off is located at the 1st piece of theoretical plate on reboiler return port.Knockout tower operating pressure 0.12MPaA, temperature are 73 DEG C, side
Line produces 135 DEG C of azeotropic mixture azeotropic temperature, glycol content 5.93wt%, the enrichment extraction of side line glycol.
It is 99.95% that separation column, which obtains 1,2- epoxy butane product purity, and the rate of recovery 99.86% separates tower bottom
Extractant purity 98.05%, extractant loss 0.89%.
[embodiment 8]
According to process flow chart shown in Fig. 1, extractant is normal octane, the object containing 1,2- epoxy butane, extractant and glycol
In stream, by weight percentage, extractant and 1, the ratio of 2- epoxy butane is 10:1, knockout tower number of theoretical plate 45, knockout tower
Side take-off is located at the 3rd piece of theoretical plate on reboiler return port.Knockout tower operating pressure 0.13MPaA, temperature are 76 DEG C, side
Line produces 137.5 DEG C of azeotropic mixture azeotropic temperature, glycol content 6.16wt%, the enrichment extraction of side line glycol.
It is 99.95% that separation column, which obtains 1,2- epoxy butane product purity, and the rate of recovery 99.87% separates tower bottom
Extractant purity 98.56%, extractant loss 0.86%.
[embodiment 9]
According to process flow chart shown in Fig. 1, extractant is normal octane, the object containing 1,2- epoxy butane, extractant and glycol
In stream, by weight percentage, extractant and 1, the ratio of 2- epoxy butane is 10:1, knockout tower number of theoretical plate 60, knockout tower
Side take-off is located at the 4th piece of theoretical plate on reboiler return port.Knockout tower operating pressure 0.15MPaA, temperature are 77 DEG C, side
Line produces 138 DEG C of azeotropic mixture azeotropic temperature, glycol content 6.21wt%, the enrichment extraction of side line glycol.
It is 99.95% that separation column, which obtains 1,2- epoxy butane product purity, and the rate of recovery 99.86% separates tower bottom
Extractant purity 98.58%, extractant loss 0.84%.
[embodiment 10]
According to process flow chart shown in Fig. 1, extractant is normal octane, the object containing 1,2- epoxy butane, extractant and glycol
In stream, by weight percentage, extractant and 1, the ratio of 2- epoxy butane is 10:1, knockout tower number of theoretical plate 80, knockout tower
Side take-off is located at the 6th piece of theoretical plate on reboiler return port.Knockout tower operating pressure 0.17MPaA, temperature are 80 DEG C, side
Line produces 142 DEG C of azeotropic mixture azeotropic temperature, glycol content 6.60wt%, the enrichment extraction of side line glycol.
It is 99.95% that separation column, which obtains 1,2- epoxy butane product purity, and the rate of recovery 99.82% separates tower bottom
Extractant purity 98.60%, extractant loss 0.80%.
[comparative example 1]
According to process flow chart shown in Fig. 2, extractant is normal octane, the object containing 1,2- epoxy butane, extractant and glycol
In stream, by weight percentage, extractant and 1, the ratio of 2- epoxy butane is 12:1, knockout tower number of theoretical plate 30.
In the case where guaranteeing with [embodiment 1] identical 1 2- epoxy butane purity and the rate of recovery, and [embodiment 1] phase
Than diol concentration is 5 times of diol concentration in tower reactor outlet extractant stream in [embodiment 1] side take-off logistics, i.e., outside
In the case where arranging equal amount impurity, extractant loss amount is 5 times of [embodiment 1].
Claims (9)
1. a kind of production method of epoxy butane, separates including the logistics containing epoxy butane, extractant and glycol in knockout tower
Step；
The knockout tower operates under conditions of being enough makes extractant and glycol formation azeotropic mixture, and
In logistics of the knockout tower side take-off containing extractant and glycol azeotropic mixture.
2. the production method of epoxy butane according to claim 1, which is characterized in that described to be enough to make extractant and glycol shape
Condition at azeotropic mixture includes: 0.02~0.40MPaA of pressure, preferably 0.10~0.20MPaA；80~180 DEG C of azeotropic mixture temperature,
It is preferred that 120~150 DEG C.
3. the production method of epoxy butane according to claim 1, which is characterized in that the knockout tower number of theoretical plate be 15~
80, preferably 20~65, more preferable 20~50.
4. the production method of epoxy butane according to claim 1, which is characterized in that azeotropic mixture described in knockout tower side take-off
Position be located at the 1st~8 piece of theoretical plate on knockout tower tower bottom reboiler return port.
5. the production method of epoxy butane according to claim 4, which is characterized in that azeotropic mixture described in knockout tower side take-off
Position be located at the 2nd~6 piece of theoretical plate on knockout tower tower bottom reboiler return port.
6. the production method of epoxy butane according to claim 5, which is characterized in that azeotropic mixture described in knockout tower side take-off
Position be located at the 2nd~4 piece of theoretical plate on knockout tower tower bottom reboiler return port.
7. the production method of epoxy butane according to claim 1, which is characterized in that it is described containing epoxy butane, extractant and
In the logistics of glycol, by weight percentage, the ratio of extractant and epoxy butane is (2~25): 1, preferably (3~20): 1,
More preferably (5~13): 1.
8. the production method of epoxy butane according to claim 1, which is characterized in that it is described containing epoxy butane, extractant and
The logistics of glycol is originated from the extraction product stream that epoxidation reaction of olefines product obtains after extracting rectifying.
9. the production method of epoxy butane according to claim 1, which is characterized in that the glycol include epoxy butane and/
Or the hydrolysate of its isomer.
Priority Applications (19)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711241136.1A CN109851587B (en) | 2017-11-30 | 2017-11-30 | Method for producing butylene oxide |
| SG11202005098UA SG11202005098UA (en) | 2017-11-30 | 2018-11-30 | Method and system for producing epoxyalkane |
| RU2020121678A RU2746482C1 (en) | 2017-11-30 | 2018-11-30 | Method and system for producing epoxyalkane |
| ES18884423T ES2942000T3 (en) | 2017-11-30 | 2018-11-30 | Production method and production system of alkylene oxide |
| BR112020010871-5A BR112020010871A2 (en) | 2017-11-30 | 2018-11-30 | method and system for the production of epoxyalkane |
| PT188844237T PT3719008T (en) | 2017-11-30 | 2018-11-30 | Alkylene oxide production method and production system |
| EP18884423.7A EP3719008B1 (en) | 2017-11-30 | 2018-11-30 | Alkylene oxide production method and production system |
| RU2020121556A RU2760003C1 (en) | 2017-11-30 | 2018-11-30 | Method and system for synthesising alkylene oxide |
| PCT/CN2018/118519 WO2019105453A1 (en) | 2017-11-30 | 2018-11-30 | Method and system for producing epoxyalkane |
| EP18883987.2A EP3719009A4 (en) | 2017-11-30 | 2018-11-30 | Method and system for producing epoxyalkane |
| JP2020529524A JP7066849B2 (en) | 2017-11-30 | 2018-11-30 | Production method and system of alkylene oxide |
| BR112020010893-6A BR112020010893A2 (en) | 2017-11-30 | 2018-11-30 | method and system for epoxyalkane production |
| US16/768,662 US11591303B2 (en) | 2017-11-30 | 2018-11-30 | Method and system for producing epoxyalkane |
| KR1020207018148A KR102458887B1 (en) | 2017-11-30 | 2018-11-30 | Method and system for production of alkylene oxide |
| PCT/CN2018/118506 WO2019105451A1 (en) | 2017-11-30 | 2018-11-30 | Alkylene oxide production method and production system |
| JP2020529567A JP7185691B2 (en) | 2017-11-30 | 2018-11-30 | Alkylene oxide production method and production system |
| US16/768,663 US11773072B2 (en) | 2017-11-30 | 2018-11-30 | Method and system for producing epoxyalkane |
| SG11202005095WA SG11202005095WA (en) | 2017-11-30 | 2018-11-30 | Method and system for producing epoxyalkane |
| KR1020207018147A KR102532058B1 (en) | 2017-11-30 | 2018-11-30 | Alkylene oxide production method and production system |
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| CN201711241136.1A CN109851587B (en) | 2017-11-30 | 2017-11-30 | Method for producing butylene oxide |
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Citations (7)
| 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 |
| JPS5924982B2 (en) * | 1979-09-26 | 1984-06-13 | 昭和電工株式会社 | Purification method of butylene oxide |
| US5529667A (en) * | 1994-12-01 | 1996-06-25 | Hoechst Celanese Corporation | Process for recovering ethylene oxide |
| CN1633424A (en) * | 2002-02-15 | 2005-06-29 | 住友化学工业株式会社 | Method of purifying propylene oxide |
| CN1678600A (en) * | 2002-07-23 | 2005-10-05 | 巴斯福股份公司 | Method for the continuous purification by distillation of 1,2-propylene glycol that accumulates during the synthesis of propylene rpoxide without coupling products |
| CN101006067A (en) * | 2004-06-23 | 2007-07-25 | 住友化学株式会社 | Method of purifying propylene oxide |
| CN104109137A (en) * | 2013-04-16 | 2014-10-22 | 中国石油化工股份有限公司 | Epoxypropane purifying method |
-
2017
- 2017-11-30 CN CN201711241136.1A patent/CN109851587B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5924982B2 (en) * | 1979-09-26 | 1984-06-13 | 昭和電工株式会社 | Purification method of butylene oxide |
| US4402794A (en) * | 1982-05-24 | 1983-09-06 | Atlantic Richfield Company | Purification of butylene oxides by extractive distillation with selected extractive distillation solvents |
| US5529667A (en) * | 1994-12-01 | 1996-06-25 | Hoechst Celanese Corporation | Process for recovering ethylene oxide |
| CN1633424A (en) * | 2002-02-15 | 2005-06-29 | 住友化学工业株式会社 | Method of purifying propylene oxide |
| CN1678600A (en) * | 2002-07-23 | 2005-10-05 | 巴斯福股份公司 | Method for the continuous purification by distillation of 1,2-propylene glycol that accumulates during the synthesis of propylene rpoxide without coupling products |
| CN101006067A (en) * | 2004-06-23 | 2007-07-25 | 住友化学株式会社 | Method of purifying propylene oxide |
| 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 |
|---|
| 王树楹主编: "《现代填料塔技术指南》", 31 August 1998, 中国石化出版社 * |
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