CN109851588A - The refining methd of propylene oxide - Google Patents
The refining methd of propylene oxide Download PDFInfo
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- CN109851588A CN109851588A CN201810153538.4A CN201810153538A CN109851588A CN 109851588 A CN109851588 A CN 109851588A CN 201810153538 A CN201810153538 A CN 201810153538A CN 109851588 A CN109851588 A CN 109851588A
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- propylene glycol
- extractant
- monomethyl ether
- dimethyl ether
- glycol dimethyl
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Abstract
The present invention relates to a kind of refining methds of propylene oxide, mainly solve the problems, such as that propylene glycol monomethyl ether, the accumulation of Propylene Glycol Dimethyl Ether heavy constituent impurity recycling in the prior art lead to that extractant purity is low, loss is big, propylene oxide yield is low, energy consumption is high.The method includes the feed streams containing propylene oxide, extractant and propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether the step of knockout tower separates；The knockout tower operates under conditions of being enough makes extractant and propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether formation azeotropic mixture, and in the knockout tower side take-off containing extractant-propylene glycol monomethyl ether azeotropic mixture and the logistics of extractant-Propylene Glycol Dimethyl Ether azeotropic mixture.The method can be used in the industrial production of propylene oxide.
Description
Technical field
The present invention relates to a kind of refining methds of propylene oxide, and in particular to propylene oxide extraction rectification technique recycling extraction
Take the purification process of agent.
Background technique
Propylene oxide (PO) is mainly used for the production of polyether polyol, propylene glycol and propylene glycol, in acryloyl derivative
Yield be only second to polypropylene, be the second largest acryloyl derivative.According to statistics, 2011, the whole world was for polyether polyols alcohol production
Propylene oxide accounts for about the 66% of aggregate consumption, accounts for about 17% for propylene glycol production, for accounting for about for propylene glycol production
6%.2011, global propylene oxide production capacity was 882.2 ten thousand tons, had broken through 10,000,000 tons within 2016.Expect the year two thousand twenty, ring
Ethylene Oxide production capacity is up to 12,000,000 tons/year, and demand reaches 10,000,000 tons/year.On long terms, world wide inner ring
Ethylene Oxide market prospects are still optimistic.
It is expected that the year demand growth amount of coming years propylene oxide is 4~8%, wherein Asian market demand may increase
Fast very fast, China and India Market increase propylene oxide consumption figure compared with other countries more swift and violent especially in recent years.It is expected that
The annual requirement of the coming five years propylene oxide is up to ten thousand tons of 1300-1400 or so.
Propylene oxide main production area in the world's is in West Europe, North America and Asia.External propylene oxide industrial concentration is very
Height, U.S.'s Dow chemistry and Lyondell company are maximum manufacturers in the world, control the major part of world's propylene oxide
Market.Dow Chemical Company has process units on the U.S., Germany, Brazil and other places respectively, is all made of chloropharin law technology.
Process units is had on the U.S., France, Holland, China and other places respectively in Lyondell company, using conjugated oxidation technology.Currently,
The world accounts for the 40~45% of aggregated capacity using the propylene oxide production capacity of chlorohydrination route, and conjugated oxidation production capacity accounts for 55~60%.
With the raising of environmental requirement, chlorohydrination will be gradually substituted.
Method as production propylene oxide, it is known to the method that cumyl hydroperoxide (or ethylbenzene) is reacted with propylene.
There is purpose reaction product propylene oxide in the reaction solution that the reaction obtains, also contains C5~C6 hydro carbons, water, aldehyde (acetaldehyde+the third
Aldehyde) and the oxygen-containing organic compounds impurity such as methanol, acetone, methyl formate.It is high therefore, it is necessary to separate, recycle from reaction solution
The multiple refining step of purity propylene oxide.
Product propylene has strict demand to water, aldehyde, and water will affect the hydroxyl value and foam performance of polymer, and aldehyde contains
Amount is environmental requirement, and C5~C6 hydro carbons will affect the coloration of product, and therefore, national standard has strict demand to product purity.
National standard oxypropylene high-class product quality purity requirement are as follows: propylene oxide >=99.95%, water≤0.02%, acetaldehyde
+ propionic aldehyde≤0.005%, acid≤0.003%.
React impurity and the propylene oxide shapes such as water, methanol, acetone, the methyl formate contained in the crude propene oxide generated
At azeotropic mixture or relative volatility close to 1, conventional distillation is difficult to reach product propylene standard.Meet in order to obtain poly-
Close desired high-purity propylene oxide, it is necessary to be separated off the impurity contained in propylene oxide.
The purifying of propylene oxide generally uses C7~C20 straight chain and branch hydro carbons and (or) glycols as extractant.From
Economy considers that the purification process of propylene oxide is using the mixture of C8 straight chain and branched paraffin as extractant.Extractant
Addition makes acetaldehyde, water, methanol, methyl formate become larger propylene oxide relative volatility, acetaldehyde, water, methanol, methyl formate from
Tower top removes.
In propylene oxide subtractive process, due to the presence of water, inevitably, propylene oxide can hydrolyze generation 1,2- third
Glycol, 1,2-PD is reacted with impurity methanol generates propylene glycol monomethyl ether, and generation is reacted in propylene glycol monomethyl ether continuation with methanol
Propylene Glycol Dimethyl Ether.If propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether are not to move out system or amount removed is less than production quantity, can make
Extractant concentration reduces, and can reduce extractant extraction efficiency, increases system energy consumption, reduces the purity of propylene oxide.Under normal pressure,
Propylene oxide boiling point is 34 DEG C, 125.7 DEG C of extractant normal octane boiling point, and propylene glycol monomethyl ether boiling point is 120.1 DEG C, propylene glycol
Dimethyl ether boiling point is 93.0 DEG C.As it can be seen that impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether boiling point are higher than propylene oxide, lower than extraction
Agent is taken, and propylene glycol monomethyl ether boiling point and normal octane are close, needs to be separately provided rectifying column separation；In addition, impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether and extractant C8 alkane form low temperature azeotropic mixture, further increase separating difficulty.
Document CN100537553C discloses a kind of purification process of propylene oxide, and this method is to make containing methyl formate
For the purification process of the propylene oxide of impurity, using C7~C20 hydrocarbon as extractant, using the method for extractive distillation, extractive distillation
Water is added in the distillate that the tower top of tower obtains, and carries out water-oil separating operation, isolated oil reservoir is reused in extraction distillation column
In, on the other hand, isolated water layer is removed to outside system, the tower bottom liquid as extraction distillation column obtains methyl formate concentration
The propylene oxide to decrease.The technology is only available for that the light component of propylene oxide can be lower than with the boiling point of extractant azeotropic
Impurity, and when split-phase impurity water allocation proportion be much larger than and impurity the impurity of extractant allocation proportion removing.
Document CN1307168C discloses a kind of refining methd of propylene oxide, and this method uses C7 in extraction distillation column
~C20 hydrocarbon extractant, to it is being reacted by isopropyl benzene hydroperoxide with propylene, containing propylene oxide and containing water, hydrocarbon and
The reaction solution of the impurity such as oxygen-containing organic compound carries out extractive distillation.And be described in detail about reduce in extractant the third two
The method of determining alcohol can enumerate the separation methods such as distillation separation, absorption, washing, settle and separate, extraction, preferably washing method point
From.
The current status of the prior art be still required it is a kind of investment it is small, extractant lose small, with high purity, propylene oxide
High income, the method for purifying propylene oxide that low energy consumption.
Summary of the invention
The present inventor passes through diligent the study found that extractant and impurity propylene glycol list first on the basis of existing technology
Ether, Propylene Glycol Dimethyl Ether form low temperature azeotropic mixture, using this azeotropic mixture and azeotropic type, by low temperature azeotropic mixture from separation
Tower side line liquid phase extraction, so that it may solve the problems, such as that at least one is aforementioned, and have thus completed the present invention.
Specifically, the present invention relates to a kind of refining methds of propylene oxide.The method includes containing propylene oxide, extraction
Take agent and propylene glycol monomethyl ether and the feed stream of Propylene Glycol Dimethyl Ether the step of knockout tower separates；
The knockout tower is being enough that extractant and propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether is made to form the condition of azeotropic mixture
Lower operation, and
Contain extractant-propylene glycol monomethyl ether azeotropic mixture and extractant-Propylene Glycol Dimethyl Ether in the knockout tower side take-off
The logistics of azeotropic mixture.
According to an aspect of the present invention, described to be enough to form extractant and propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether
The condition of azeotropic mixture includes: tower top 0.02~0.70MPaG of operating pressure, preferably 0.03~0.50MPaG；Tower top operation temperature
38~110 DEG C, preferably 42~70 DEG C.
According to an aspect of the present invention, the knockout tower number of theoretical plate N is 15~80, preferably 20~65, more preferable 20
~50.
According to an aspect of the present invention, in the feed stream, the weight ratio of extractant and propylene oxide be (2~
20): 1, preferably (3~15): 1, more preferable (5~10): 1；By weight percentage, propylene glycol monomethyl ether and propylene glycol diformazan
The total content of ether is 0.001~2.0%, preferably 0.001~1.5%, more preferable 0.001~1.0%.
According to an aspect of the present invention, the feed stream is originated from propylene ring oxidation reaction product after extracting rectifying
Obtained extraction product stream.
According to an aspect of the present invention, described in knockout tower side take-off containing extractant-propylene glycol monomethyl ether azeotropic mixture and
Position of the position of extractant-Propylene Glycol Dimethyl Ether azeotropic mixture logistics between 0.01N~0.95N, preferably
Position between 0.05N~0.85N.
According to an aspect of the present invention, the described of knockout tower side take-off contains extractant-propylene glycol monomethyl ether azeotropic mixture
With the flow of extractant-Propylene Glycol Dimethyl Ether azeotropic mixture logistics, with propylene glycol monomethyl ether contained by the feed stream and the third two
The ratio of diethylene glycol dimethyl ether flow is (1~10): 1, preferably (1~8): 1, more preferable (1~4): 1.
According to an aspect of the present invention, knockout tower side line is divided at least two strands, and extraction is rich in extractant-propylene glycol respectively
First logistics of monomethyl ether azeotropic mixture, and rich in the second logistics of extractant-Propylene Glycol Dimethyl Ether azeotropic mixture.
According to an aspect of the present invention, second logistics adopts outlet port and is configured at the first logistics extraction mouth
Top.
According to an aspect of the present invention, the extraction of knockout tower side line sub-thread containing extractant-propylene glycol monomethyl ether azeotropic mixture and
Extractant-Propylene Glycol Dimethyl Ether azeotropic mixture third―party logistics.
According to an aspect of the present invention, the method also includes: it is described containing extractant-propylene glycol monomethyl ether azeotropic mixture,
The logistics of extractant-Propylene Glycol Dimethyl Ether azeotropic mixture enters phase-splitter, and the light phase logistics rich in extractant is obtained after split-phase, and
Heavy phase logistics rich in propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether；The light phase logistics returns to the knockout tower, the heavy phase
Logistics extraction.
According to an aspect of the present invention, described to contain extractant-propylene glycol monomethyl ether azeotropic mixture and extractant-propylene glycol
The logistics of dimethyl ether azeotropic mixture enters the phase-splitter after being cooled to 35~60 DEG C.
Beneficial effects of the present invention: the method for the present invention is recombinated using extractant and propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether
Impurity is divided to form azeotropic mixture, from knockout tower side take-off azeotropic mixture, thus by propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether impurity
Be discharged from extractant circulating system, decontamination cycle extractant improves extractant purity, reduce extractant loss and
Energy consumption improves the yield of propylene oxide.With the prior art directly by the scheme of knockout tower tower reactor stream portions outlet compared with,
Extractant purity improves 0.1~14%, and extractant only loses 0.05~1%, and energy consumption reduces 1~16%, and propylene oxide is received
Rate improves 0.5~5%.
Detailed description of the invention
Fig. 1 is the flow diagram of one embodiment of the present invention.
Fig. 2 is the flow diagram of another embodiment of the present invention.
Fig. 3 is the flow diagram of another embodiment of the present invention.
Fig. 4 is comparative example flow diagram.
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 product propylene logistics
4 reboiler feed streams
5 reboiler output streams
7 containing extractant-propylene glycol monomethyl ether azeotropic mixture and extractant-Propylene Glycol Dimethyl Ether azeotropic mixture logistics (third
Logistics)
Logistics after 8 coolings
9 are rich in the light phase logistics of extractant
10 are rich in the heavy phase logistics of propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether
11 contaminant streams
12 are rich in extractant-Propylene Glycol Dimethyl Ether azeotropic mixture side take-off logistics (the second logistics)
13 are rich in extractant-propylene glycol monomethyl ether azeotropic mixture side take-off logistics (the first logistics)
A knockout tower
B reboiler
C cooler
D phase-splitter
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., it is conventional that object derived from the prefix covers this field when the application proposes
Those of use, 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 is equal
It is considered as a part of the original disclosure of the present invention or original description, and is not considered as not disclosing or being expected herein new
Content, unless those skilled in the art think that the combination is obvious unreasonable.
In the case where not clearly indicating, all percentages, number, ratio for being previously mentioned in this specification etc. are all
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, the number of theoretical plate being previously mentioned in this specification is all to calculate from top to bottom, i.e.,
Overhead condenser is first piece of theoretical plate, and tower reactor reboiler is last block theoretical plate.
In the case where not clearly indicating, the pressure being previously mentioned in this specification refers to relative pressure.
Raw material used in purification process of the invention is the logistics containing propylene oxide and extractant.The logistics is originated from propylene
The extraction product stream that epoxidation reaction product obtains after extractive distillation column (attached drawing of the present invention is not directed to) extracting rectifying.The object
In stream, the weight ratio of extractant and propylene oxide is (2~20): 1, preferably (3~15): 1, more preferable (5~10): 1；With weight
Measure percentages, the total content of propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether is 0.001~2.0%, preferably 0.001~
1.5%, more preferable 0.001~1.0%.
The extractant that oxide purification 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, example
Such as normal octane, isooctane, 2- methyl heptane.From extractant cost consideration is reduced, mixture is preferably selected.
According to the present invention, in Fig. 1, containing propylene oxide, extractant and impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether
Logistics 1 enters knockout tower A, and product propylene logistics 3 is removed from separation column, and extractant stream 2 is moved from separation tower bottom
Out, the extractive distillation column (attached drawing of the present invention is not directed to) that the extractant of removal can return to preamble is recycled.The bottom knockout tower A
Portion is equipped with reboiler B, and tower bottoms is sent into reboiler B, reboiler B output streams are obtained after heating by reboiler B feed stream 4
5, output streams 5 send the lower part knockout tower A back to, contain extractant-propylene glycol monomethyl ether azeotropic mixture and extractant-Propylene Glycol Dimethyl Ether
The side take-off logistics 7 of azeotropic mixture is from knockout tower A side take-off.As a result, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether from
It is discharged in system.
The present inventor has found that extractant-propylene glycol monomethyl ether azeotropic mixture, extractant-Propylene Glycol Dimethyl Ether are total after study
Boiling object is minimum temperature azeotrope, and azeotropic mixture type is heterogeneous azeotrope.By taking extractant is normal octane as an example, under normal pressure
Normal octane boiling point is 125.7 DEG C, and propylene glycol monomethyl ether boiling point is 120.1 DEG C, and Propylene Glycol Dimethyl Ether boiling point is 93.0 DEG C；It is just pungent
Alkane-propylene glycol monomethyl ether azeotropic mixture temperature is 103.7 DEG C, azeotropic composition are as follows: normal octane 55.67wt%, propylene glycol monomethyl ether
44.33wt%；Normal octane-Propylene Glycol Dimethyl Ether azeotropic mixture temperature is 92.4 DEG C, azeotropic composition are as follows: normal octane 11.89wt%,
Propylene Glycol Dimethyl Ether 88.11wt%.Minimum temperature azeotrope can use by side take-off, the heterogeneous azeotrope of extraction
Simply, Phase separation technique inexpensively efficiently separates impurity, while recycling extractant, recycles.
It extracts agent content with pressure rise, in extractant-propylene glycol monomethyl ether azeotropic mixture to be gradually reduced, propylene glycol list
Methyl ether content is gradually increasing；And extractant-Propylene Glycol Dimethyl Ether azeotropic mixture, but with pressure rise, extractant contains in azeotropic mixture
Amount is gradually increasing, and impurity Propylene Glycol Dimethyl Ether content is gradually reduced.So with pressure rise, impurity propylene glycol in azeotropic mixture
Monomethyl ether content is gradually increasing, and impurity Propylene Glycol Dimethyl Ether content is gradually reduced.That is, with pressure rise, in side
In the identical situation of line produced quantity, the impurity propylene glycol monomethyl ether of extraction increases, and impurity Propylene Glycol Dimethyl Ether is reduced.Therefore,
It needs to select suitable pressure, so that extractant loss reduction.Comprehensively consider preferably 0.03~0.50MPaG, corresponding azeotropic mixture
Preferably 100~160 DEG C of temperature.Optimal extraction composition is exactly the corresponding azeotropic composition of operating pressure, otherwise side take-off group
It will increase at the amount of middle extractant, directly dump loss amount increase.
Produce the position containing extractant-propylene glycol monomethyl ether azeotropic mixture, the logistics of extractant-Propylene Glycol Dimethyl Ether azeotropic mixture
Position setting in the position between 0.01N~0.95N, between preferably 0.05N~0.85N.In this position, azeotropic
Propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content highest in object composition, the amount of the propylene oxide and extractant taken out of are minimum.More
Up, azeotropic mixture composition oxypropylene and extractant concentration are higher, and impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether are dense
Degree is lower, and the propylene oxide and extractant taken out of when producing azeotropic mixture are more, loses bigger.
The extraction of side line azeotropic mixture can be produced with sub-thread, can also be divided to two bursts of extraction, preferably sub-thread side take-off.Equally with
For normal octane, normal octane-propylene glycol monomethyl ether azeotropic mixture boiling point is lower than 20~40 DEG C of normal octane, normal octane-propylene glycol diformazan
Ether azeotropic mixture boiling point is lower than 30~45 DEG C of normal octane, therefore, (attached drawing 2), side take-off in another embodiment of the present invention
Logistics number of share of stock is consistent with dopant species number.In raw material of the present invention, there are two types of impurity, therefore side take-off is two strands.Two strands of side lines are adopted
It is respectively out: rich in the first logistics of extractant-propylene glycol monomethyl ether azeotropic mixture, and is rich in extractant-Propylene Glycol Dimethyl Ether
Second logistics of azeotropic mixture.In first logistics, including extractant-propylene glycol monomethyl ether azeotropic mixture, extractant-propylene glycol diformazan
Ether azeotropic mixture, but it is rich in extractant-propylene glycol monomethyl ether azeotropic mixture, and is extractant-propylene glycol monomethyl ether azeotropic mixture
Middle propylene glycol monomethyl ether concentration highest point.In second logistics, including extractant-propylene glycol monomethyl ether azeotropic mixture, extractant-the third
Glycol dimethyl ether azeotropic mixture, but it is rich in extractant-Propylene Glycol Dimethyl Ether azeotropic mixture, and is extractant-propylene glycol two
Propylene Glycol Dimethyl Ether concentration highest point in methyl ether azeotropic mixture.Second logistics adopts outlet port and is configured at the first logistics extraction mouth
Top.
Fig. 3 is a preferred embodiment of the present invention.Containing extractant-propylene glycol monomethyl ether azeotropic mixture and extractant-the third
Enter phase-splitter after the logistics 7 of glycol dimethyl ether azeotropic mixture is cooling, the light phase logistics rich in extractant is obtained after split-phase, and rich
Heavy phase logistics containing propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether；Light phase logistics returns to knockout tower, heavy phase logistics extraction.By side
The line extraction technical solution that the light phase rich in extractant returns to knockout tower after cooling split-phase can greatly improve the pure of extractant
Degree, while reducing the loss of extractant.
Fig. 4 is the prior art, and the logistics 1 containing propylene oxide, extractant and impurity enters knockout tower A, product propylene
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
It boils device B feed stream 4 and tower bottoms is sent into reboiler B, reboiler B output streams 5 are obtained after heating, output streams 5, which are sent into, to be divided
From the lower part tower A, extractant stream 2 separates one logistics 11, takes this for impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether to be discharged
System.Due to passing through the tower reactor logistics of outlet part to reduce accumulation of the impurity in extractant, thus larger amount of extraction can be lost
Take agent.
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 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 1.0%, extractant and 1, the ratio of 2- propylene oxide is 2.1:1, knockout tower number of theoretical plate 20, knockout tower side take-off position
In the 7th piece of theoretical plate.Knockout tower operating pressure 0.02MPaG, temperature be 40 DEG C, 100 DEG C of side take-off temperature, impurity propylene glycol
Monomethyl ether and Propylene Glycol Dimethyl Ether content 52.85wt%, side line impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment are adopted
Out.
According to process flow shown in Fig. 1, it is 99.95% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.95% separates tower bottom extractant purity 99.79%, extractant loss 0.210%.
According to process flow shown in Fig. 2, side take-off position selects impurity propylene glycol monomethyl ether and propylene glycol diformazan respectively
Ether content maximum, i.e. the 17th piece of theoretical plate produce impurity propylene glycol monomethyl ether, herein 112 DEG C of azeotropic temperature, impurity propylene glycol
Monomethyl ether content 38.73%, impurity Propylene Glycol Dimethyl Ether content 0.25%；5th block of plate produces impurity Propylene Glycol Dimethyl Ether, this
78 DEG C of azeotropic temperature of place, propylene glycol monomethyl ether content 15.64%, Propylene Glycol Dimethyl Ether content 38.27%, two strands of extraction impurity
Total amount 47.20%.
According to process flow shown in Fig. 2, it is 99.95% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.90% separates tower bottom extractant purity 99.78%, extractant loss 0.207%.
In the case where side take-off total amount is the same, according to the ratio of process flow shown in Fig. 1 according to process flow shown in Fig. 2
Than more extraction impurity 11.86%, in the process flow as shown in Fig. 2,1,2- propylene oxide increases from side take-off amount, therefore 1,
The decline of the 2- propylene oxide rate of recovery, the loss late of extractant slightly decline.
[embodiment 2]
According to process flow shown in Fig. 1, extractant is normal octane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 1.0%, extractant and 1, the ratio of 2- propylene oxide is 2.1:1, knockout tower number of theoretical plate 20, knockout tower side take-off position
In the 7th piece of theoretical plate.Knockout tower operating pressure 0.05MPaG, temperature be 46 DEG C, 106 DEG C of side take-off temperature, impurity propylene glycol
Monomethyl ether and Propylene Glycol Dimethyl Ether content 52.58wt%, side line impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment are adopted
Out.
It is 99.95% that separation column, which obtains 1,2- product propylene purity, and the rate of recovery 99.94% separates tower bottom
Extractant purity 99.79%, extractant loss 0.210%.
[embodiment 3]
According to process flow shown in Fig. 1, extractant is normal octane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 1.0%, extractant and 1, the ratio of 2- propylene oxide is 2.1:1, knockout tower number of theoretical plate 20, knockout tower side take-off position
In the 7th piece of theoretical plate.Knockout tower operating pressure 0.10MPaG, temperature be 55 DEG C, 116 DEG C of side take-off temperature, impurity propylene glycol
Monomethyl ether and Propylene Glycol Dimethyl Ether content 52.10wt%, side line impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment are adopted
Out.
It is 99.95% that separation column, which obtains 1,2- product propylene purity, and the rate of recovery 99.93% separates tower bottom
Extractant purity 99.79%, extractant loss 0.211%.
[embodiment 4]
According to process flow shown in Fig. 1, extractant is normal octane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 1.0%, extractant and 1, the ratio of 2- propylene oxide is 2.1:1, knockout tower number of theoretical plate 20, knockout tower side take-off position
In the 7th piece of theoretical plate.Knockout tower operating pressure 0.25MPaG, temperature be 74 DEG C, 135 DEG C of side take-off temperature, impurity propylene glycol
Monomethyl ether and Propylene Glycol Dimethyl Ether content 50.83wt%, side line impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment are adopted
Out.
It is 99.95% that separation column, which obtains 1,2- product propylene purity, and the rate of recovery 99.92% separates tower bottom
Extractant purity 99.78%, extractant loss 0.215%.
[embodiment 5]
According to process flow shown in Fig. 1, extractant is normal octane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 1.0%, extractant and 1, the ratio of 2- propylene oxide is 2.1:1, knockout tower number of theoretical plate 20, knockout tower side take-off position
In the 7th piece of theoretical plate.Knockout tower operating pressure 0.50MPaG, temperature be 96 DEG C, 161 DEG C of side take-off temperature, impurity propylene glycol
Monomethyl ether and Propylene Glycol Dimethyl Ether content 49.5wt%, side line impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment are adopted
Out.
It is 99.95% that separation column, which obtains 1,2- product propylene purity, and the rate of recovery 99.90% separates tower bottom
Extractant purity 99.78%, extractant loss 0.221%.
[embodiment 6]
According to process flow shown in Fig. 1, extractant is normal octane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 1.0%, extractant and 1, the ratio of 2- propylene oxide is 2.1:1, knockout tower number of theoretical plate 20, knockout tower side take-off position
In the 7th piece of theoretical plate.Knockout tower operating pressure 0.65MPaG, temperature are 105 DEG C, 166 DEG C of side take-off temperature, impurity the third two
Alcohol monomethyl ether and Propylene Glycol Dimethyl Ether content 49.06wt%, side line impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment
Extraction.
It is 99.95% that separation column, which obtains 1,2- product propylene purity, and the rate of recovery 99.89% separates tower bottom
Extractant purity 99.77%, extractant loss 0.225%.
[embodiment 7]
According to process flow shown in Fig. 1, extractant is normal octane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 1.0%, extractant and 1, the ratio of 2- propylene oxide is 5:1, knockout tower number of theoretical plate 30, and knockout tower side take-off is located at the
8 pieces of theoretical plates.Knockout tower operating pressure 0.02MPaG, temperature be 40 DEG C, 107 DEG C of side take-off temperature, impurity propylene glycol list first
Ether and Propylene Glycol Dimethyl Ether content 54.85wt%, side line impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment extraction.
According to process flow shown in Fig. 1, it is 99.99% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.99% separates tower bottom extractant purity 99.89%, extractant loss 0.109%.
[embodiment 8]
According to process flow shown in Fig. 1, extractant is normal octane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 1.5%, extractant and 1, the ratio of 2- propylene oxide is 10:1, knockout tower number of theoretical plate 40, and knockout tower side take-off is located at
8th piece of theoretical plate.Knockout tower operating pressure 0.02MPaG, temperature be 40 DEG C, 101 DEG C of side take-off temperature, impurity propylene glycol list
Methyl ether and Propylene Glycol Dimethyl Ether content 55.35wt%, side line impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment extraction.
According to process flow shown in Fig. 1, it is 99.97% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.97% separates tower bottom extractant purity 99.96%, extractant loss 0.0428%.
[embodiment 9]
According to process flow shown in Fig. 1, extractant is normal octane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 1.5%, extractant and 1, the ratio of 2- propylene oxide is 15:1, knockout tower number of theoretical plate 50, and knockout tower side take-off is located at
10th piece of theoretical plate.Knockout tower operating pressure 0.02MPaG, temperature be 40 DEG C, 102 DEG C of side take-off temperature, impurity propylene glycol
Monomethyl ether and Propylene Glycol Dimethyl Ether content 55.48wt%, side line impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment are adopted
Out.
According to process flow shown in Fig. 1, it is 99.97% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.97% separates tower bottom extractant purity 99.97%, extractant loss 0.0285%.
[embodiment 10]
According to process flow shown in Fig. 1, extractant is 2- methyl heptane, contains 1,2- propylene oxide, extractant and impurity third
Glycol monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether
Content is 1.5%, extractant and 1, and the ratio of 2- propylene oxide is 2.1:1, knockout tower number of theoretical plate 20, and knockout tower side line is adopted
It is located at the 6th piece of theoretical plate out.Knockout tower operating pressure 0.02MPaG, temperature be 40 DEG C, 91 DEG C of side take-off temperature, impurity third
Glycol monomethyl ether and Propylene Glycol Dimethyl Ether content 46.91wt%, side line impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether are rich
Collection extraction.
According to process flow shown in Fig. 1, it is 99.95% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.91% separates tower bottom extractant purity 99.75%, extractant loss 0.247%.
[embodiment 11]
According to process flow shown in Fig. 1, extractant is isooctane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 1.5%, extractant and 1, the ratio of 2- propylene oxide is 2.1:1, knockout tower number of theoretical plate 20, knockout tower side take-off position
In the 16th piece of theoretical plate.Knockout tower operating pressure 0.02MPaG, temperature be 40 DEG C, 97 DEG C of side take-off temperature, impurity propylene glycol
Monomethyl ether and Propylene Glycol Dimethyl Ether content 27.63wt%, side line impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment are adopted
Out.
According to process flow shown in Fig. 1, it is 99.95% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.90% separates tower bottom extractant purity 99.64%, extractant loss 0.360%.
[embodiment 12]
According to process flow shown in Fig. 3, extractant is normal octane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 0.8%, extractant and 1, the ratio of 2- propylene oxide is 2.1:1, knockout tower number of theoretical plate 20, knockout tower side take-off position
In the 9th piece of theoretical plate.
Side take-off azeotrope stream flow is the 1.5:1 of feed stream impurities flow；Side take-off azeotropic mixture pressure
Power 0.028MPaG, 104 DEG C of azeotropic temperature, impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether content 50.26wt%, side line are miscellaneous
Matter propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment extraction.
According to process flow shown in Fig. 3, it is 99.96% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.96% separates tower bottom extractant purity 99.88%, extractant loss 0.1523%.
[embodiment 13]
According to process flow shown in Fig. 3, extractant is normal octane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 0.8%, extractant and 1, the ratio of 2- propylene oxide is 2.1:1, knockout tower number of theoretical plate 20, knockout tower side take-off position
In the 14th piece of theoretical plate.
Side take-off azeotrope stream flow is the 2.5:1 of feed stream impurities flow；Side take-off azeotropic mixture pressure
Power 0.034MPaG, 109 DEG C of azeotropic temperature, impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether content 46.35wt%, side line are miscellaneous
Matter propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment extraction.
According to process flow shown in Fig. 3, it is 99.99% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.99% separates tower bottom extractant purity 99.99%, extractant loss 0.1546%.
[embodiment 14]
According to process flow shown in Fig. 3, extractant is normal octane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 0.8%, extractant and 1, the ratio of 2- propylene oxide is 2.1:1, knockout tower number of theoretical plate 20, knockout tower side take-off position
In the 14th piece of theoretical plate.
Side take-off azeotrope stream flow is the 3.5:1 of feed stream impurities flow；Side take-off azeotropic mixture pressure
Power 0.034MPaG, 108 DEG C of azeotropic temperature, impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether content 37.02wt%, side line are miscellaneous
Matter propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment extraction.
According to process flow shown in Fig. 3, it is 99.99% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.99% separates tower bottom extractant purity 99.99%, extractant loss 0.1550%.
[embodiment 15]
According to process flow shown in Fig. 3, extractant is normal octane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 0.8%, extractant and 1, the ratio of 2- propylene oxide is 2.1:1, knockout tower number of theoretical plate 20, and knockout tower side take-off is located at
14th piece of theoretical plate.
Side take-off azeotrope stream flow is the 4.5:1 of feed stream impurities flow；Side take-off azeotropic mixture pressure
Power 0.034MPaG, 108 DEG C of azeotropic temperature, impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether content 31.84wt%, side line are miscellaneous
Matter propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment extraction.
According to process flow shown in Fig. 3, it is 99.99% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.99% separates tower bottom extractant purity 99.99%, extractant loss 0.1552%.
[embodiment 16]
According to process flow shown in Fig. 3, extractant is normal octane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 0.8%, extractant and 1, the ratio of 2- propylene oxide is 2.1:1, knockout tower number of theoretical plate 20, knockout tower side take-off position
In the 14th piece of theoretical plate.
Side take-off azeotrope stream flow is the 8:1 of feed stream impurities flow；Side take-off azeotropic mixture pressure
0.034MPaG, 108 DEG C of azeotropic temperature, impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether content 23.90wt%, side line impurity
Propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment extraction.
According to process flow shown in Fig. 3, it is 99.99% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.99% separates tower bottom extractant purity 99.99%, extractant loss 0.1556%.
[embodiment 17]
According to process flow shown in Fig. 3, extractant is normal octane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 0.8%, extractant and 1, the ratio of 2- propylene oxide is 4:1, knockout tower number of theoretical plate 30, and knockout tower side take-off is located at
21st piece of theoretical plate.
Side take-off azeotrope stream flow is the 4.5:1 of feed stream impurities flow；Side take-off azeotropic mixture pressure
Power 0.034MPaG, 108 DEG C of azeotropic temperature, impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether content 31.94wt%, side line are miscellaneous
Matter propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment extraction.
According to process flow shown in Fig. 3, it is 99.99% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.99% separates tower bottom extractant purity 99.99%, extractant loss 0.1492%.
[embodiment 18]
According to process flow shown in Fig. 3, extractant is normal octane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 0.8%, extractant and 1, the ratio of 2- propylene oxide is 7:1, knockout tower number of theoretical plate 35, and knockout tower side take-off is located at
21st piece of theoretical plate.
Side take-off azeotrope stream flow is the 4.5:1 of feed stream impurities flow；Side take-off azeotropic mixture pressure
Power 0.314MPaG, 151 DEG C of azeotropic temperature, impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether content 31.92wt%, side line are miscellaneous
Matter propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment extraction.
According to process flow shown in Fig. 3, it is 99.99% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.99% separates tower bottom extractant purity 99.99%, extractant loss 0.1153%.
[embodiment 19]
According to process flow shown in Fig. 3, extractant is normal octane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 0.8%, extractant and 1, the ratio of 2- propylene oxide is 9:1, knockout tower number of theoretical plate 45, and knockout tower side take-off is located at
21st piece of theoretical plate.
Side take-off azeotrope stream flow is the 4.5:1 of feed stream impurities flow；Side take-off azeotropic mixture pressure
Power 0.514MPaG, 168 DEG C of azeotropic temperature, impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether content 31.89wt%, side line are miscellaneous
Matter propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment extraction.
According to process flow shown in Fig. 3, it is 99.99% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.99% separates tower bottom extractant purity 99.99%, extractant loss 0.1055%.
[embodiment 20]
According to process flow shown in Fig. 3, extractant is 2- methyl heptane, contains 1,2- propylene oxide, extractant and impurity third
Glycol monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether
Content is 0.8%, extractant and 1, and the ratio of 2- propylene oxide is 2.1:1, knockout tower number of theoretical plate 20, and knockout tower side line is adopted
It is located at the 10th piece of theoretical plate out.
Side take-off azeotrope stream flow is the 4.5:1 of feed stream impurities flow；Side take-off azeotropic mixture pressure
Power 0.03MPaG, 103 DEG C of azeotropic temperature, impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether content 40.77wt%, side line are miscellaneous
Matter propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment extraction.
According to process flow shown in Fig. 3, it is 99.95% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.88% separates tower bottom extractant purity 99.75%, extractant loss 1.086%%.
[embodiment 21]
According to process flow shown in Fig. 3, extractant is isooctane, contains 1,2- propylene oxide, extractant and impurity propylene glycol
Monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether content
It is 0.8%, extractant and 1, the ratio of 2- propylene oxide is 2.1:1, knockout tower number of theoretical plate 30, knockout tower side take-off position
In the 9th piece of theoretical plate.
Side take-off azeotrope stream flow is the 4.5:1 of feed stream impurities flow；Side take-off azeotropic mixture pressure
Power 0.03MPaG, 95 DEG C of azeotropic temperature, impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether content 26.11wt%, side line impurity
Propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether enrichment extraction.
According to process flow shown in Fig. 3, it is 99.95% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.98% separates tower bottom extractant purity 99.56%, extractant loss 1.451%.
[comparative example 1]
According to process flow chart shown in Fig. 4, extractant is normal octane, containing 1,2- propylene oxide, extractant and impurity the third two
Alcohol monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether contain
Amount is 0.8%, extractant and 1, and the ratio of 2- propylene oxide is 2.1:1, knockout tower number of theoretical plate 20, the extraction of knockout tower tower reactor
Contaminant stream.Knockout tower operating pressure 0.02MPaG, temperature are 40 DEG C, and tower reactor produces 134 DEG C of contaminant stream temperature, impurity third
Glycol monomethyl ether and Propylene Glycol Dimethyl Ether content 0.478wt%, impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether extraction.
According to process flow shown in Fig. 4, it is 99.99% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.99% separates tower bottom extractant purity 99.52%, extractant loss 0.479%.
[comparative example 2]
According to process flow chart shown in Fig. 4, extractant is 2- methyl heptane, contains 1,2- propylene oxide, extractant and impurity
Propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether logistics in, by weight percentage, impurity propylene glycol monomethyl ether, propylene glycol diformazan
Ether content is 0.8%, extractant and 1, and the ratio of 2- propylene oxide is 2.1:1, knockout tower number of theoretical plate 20, knockout tower tower reactor
Produce contaminant stream.Knockout tower operating pressure 0.02MPaG, temperature are 40 DEG C, and 127 DEG C of contaminant stream temperature of tower reactor extraction is miscellaneous
Matter propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether content 0.478wt%, impurity propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether are adopted
Out.
According to process flow shown in Fig. 4, it is 99.99% that separation column, which obtains 1,2- product propylene purity, recycling
Rate 99.99% separates tower bottom extractant purity 99.52%, extractant loss 0.479%.
Claims (12)
1. a kind of refining methd of propylene oxide, including contain propylene oxide, extractant and propylene glycol monomethyl ether and propylene glycol two
The feed stream of methyl ether is the step of knockout tower separates；
The knockout tower is grasped under conditions of being enough makes extractant and propylene glycol monomethyl ether, Propylene Glycol Dimethyl Ether formation azeotropic mixture
Make, and
Contain extractant-propylene glycol monomethyl ether azeotropic mixture and extractant-Propylene Glycol Dimethyl Ether azeotropic in the knockout tower side take-off
The logistics of object.
2. the refining methd of propylene oxide according to claim 1, which is characterized in that described to be enough to make extractant and propylene glycol
It includes: tower top 0.02~0.70MPaG of operating pressure that monomethyl ether, Propylene Glycol Dimethyl Ether, which form the condition of azeotropic mixture, preferably 0.03~
0.50MPaG；38~110 DEG C of tower top operation temperature, preferably 42~70 DEG C.
3. the refining methd of propylene oxide according to claim 1, which is characterized in that the knockout tower number of theoretical plate N is 15
~80, preferably 20~65, more preferable 20~50.
4. the refining methd of propylene oxide according to claim 1, which is characterized in that in the feed stream, extractant with
The weight ratio of propylene oxide is (2~20): 1, preferably (3~15): 1, more preferable (5~10): 1；By weight percentage, the third two
Alcohol monomethyl ether and the total content of Propylene Glycol Dimethyl Ether be 0.001~2.0%, preferably 0.001~1.5%, more preferable 0.001~
1.0%.
5. the refining methd of propylene oxide according to claim 1, which is characterized in that the feed stream is originated from propylene epoxy
Change the extraction product stream that reaction product obtains after extracting rectifying.
6. the refining methd of propylene oxide according to claim 1, which is characterized in that containing extraction described in knockout tower side take-off
The position of agent-propylene glycol monomethyl ether azeotropic mixture and the logistics of extractant-Propylene Glycol Dimethyl Ether azeotropic mixture be located at 0.01N~
Position between 0.95N, the position between preferably 0.05N~0.85N.
7. the refining methd of propylene oxide according to claim 1, which is characterized in that the described of knockout tower side take-off contains extraction
The flow for taking agent-propylene glycol monomethyl ether azeotropic mixture and the logistics of extractant-Propylene Glycol Dimethyl Ether azeotropic mixture, with the feed stream
The ratio of contained propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether flow is (1~10): 1, preferably (1~8): 1, more preferably (1~
4):1。
8. the refining methd of propylene oxide according to claim 1, which is characterized in that knockout tower side line is divided at least two strands, point
It Cai Chu be rich in the first logistics of extractant-propylene glycol monomethyl ether azeotropic mixture, and be rich in extractant-Propylene Glycol Dimethyl Ether azeotropic mixture
The second logistics.
9. the refining methd of propylene oxide according to claim 8, which is characterized in that second logistics is adopted outlet port and matched
It is placed in the top of the first logistics extraction mouth.
10. the refining methd of propylene oxide according to claim 1, which is characterized in that the extraction of knockout tower side line sub-thread is containing extraction
Take agent-propylene glycol monomethyl ether azeotropic mixture and extractant-Propylene Glycol Dimethyl Ether azeotropic mixture third―party logistics.
11. the refining methd of propylene oxide according to claim 1, which is characterized in that the method also includes: it is described containing extraction
It takes agent-propylene glycol monomethyl ether azeotropic mixture and the logistics of extractant-Propylene Glycol Dimethyl Ether azeotropic mixture to enter phase-splitter, is obtained after split-phase
Light phase logistics rich in extractant, and the heavy phase logistics rich in propylene glycol monomethyl ether and Propylene Glycol Dimethyl Ether；The light phase logistics
Return to the knockout tower, the heavy phase logistics extraction.
12. the refining methd of propylene oxide according to claim 11, which is characterized in that described to contain extractant-propylene glycol list
Methyl ether azeotropic mixture and the logistics of extractant-Propylene Glycol Dimethyl Ether azeotropic mixture enter the phase-splitter after being cooled to 35~60 DEG C.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1307168A (en) * | 2000-01-27 | 2001-08-08 | 张立民 | Hooked-head lock |
| CN104109137A (en) * | 2013-04-16 | 2014-10-22 | 中国石油化工股份有限公司 | Epoxypropane purifying method |
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| CN1307168A (en) * | 2000-01-27 | 2001-08-08 | 张立民 | Hooked-head lock |
| CN104109137A (en) * | 2013-04-16 | 2014-10-22 | 中国石油化工股份有限公司 | Epoxypropane purifying method |
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| CN110330413A (en) * | 2019-07-31 | 2019-10-15 | 惠生工程（中国）有限公司 | A method of propylene glycol monomethyl ether in recycling alcohol ether aqueous solution logistics |
| CN110330413B (en) * | 2019-07-31 | 2022-08-09 | 惠生工程（中国）有限公司 | Method for recovering propylene glycol monomethyl ether in alcohol ether aqueous solution material flow |
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