CN106397364B - The purification devices of propylene oxide - Google Patents
The purification devices of propylene oxide Download PDFInfo
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- CN106397364B CN106397364B CN201510468102.0A CN201510468102A CN106397364B CN 106397364 B CN106397364 B CN 106397364B CN 201510468102 A CN201510468102 A CN 201510468102A CN 106397364 B CN106397364 B CN 106397364B
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D303/00—Compounds containing three-membered rings having one oxygen atom as the only ring hetero atom
- C07D303/02—Compounds containing oxirane rings
- C07D303/04—Compounds containing oxirane rings containing only hydrogen and carbon atoms in addition to the ring oxygen atoms
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D301/00—Preparation of oxiranes
- C07D301/32—Separation; Purification
Abstract
The present invention relates to a kind of purification devices of propylene oxide, the prior art is mainly solved due to medium outside introducing system, cause extractant at high cost, and do not take into account recycling methanol, or recycling methanol due to concentration is not high and the problem of be unable to Recycling and lead to material waste.The present invention is by using including: a) the first mixer；Contact impure crude propene oxide with aqueous slkali, the first logistics is obtained；B) the second mixer；Contact first logistics with hydrazine or hydrazine hydrate, the second logistics is obtained；C) low-pressure distillation tower；For separating to second logistics, tower top obtains third―party logistics, the methanol stream that tower side line is recycled, and tower reactor obtains heavy constituent logistics；D) high-pressure rectification tower；For separating to the third―party logistics, tower top obtains the 4th logistics, and tower reactor obtains product propylene；The technical solution that 4th logistics is recycled back to the low-pressure distillation tower preferably solves the problems, such as this, can be used in the industrial production of oxide purification.
Description
Technical field
The present invention relates to a kind of purification devices of propylene oxide more particularly to a kind of hydrogen peroxide direct oxidation methods (HPPO)
The crude propene oxide purification devices containing impurity such as water, methanol, acetaldehyde, acetone, methyl formates of production.
Background technique
Propylene oxide is important organic compound raw material, mainly for the production of polyether polyol, propylene glycol and all kinds of non-
Ionic surface active agent etc., wherein polyether polyol is production polyurethane foam, thermal insulation material, elastomer, adhesive and coating
Deng important source material, all kinds of nonionic surface active agent are answered extensively in industries such as petroleum, chemical industry, pesticide, weaving, daily use chemicals
With.However only the propylene oxide with higher degree can be used to manufacture polyvalent alcohol, therefore will be to the epoxy third of synthesis
Alkane crude product can be applied to prepare polyvalent alcohol after carrying out purification processes.And propylene oxide occurs to polymerize desired condition,
Propene oxide purity is not required nothing more than and reaches 99.95 weight %, has strict demand to water impurity, aldehyde, non-volatile point of content.
Hydrogen peroxide direct oxidation method (HPPO method) is under the action of molecular sieve catalyst, using double in methanol solution
The method of oxygen water direct oxidation propylene synthesizing epoxypropane.The crude propene oxide obtained after Propylene recovery, separating by-products,
Still containing impurity such as methanol, acetaldehyde, acetone, methyl formate and water.Meet the high-purity propylene oxide that polymerization requires in order to obtain,
The impurity contained in propylene oxide must be separated off.Since methyl formate and propylene oxide relative volatility are close to 1, second
The features such as aldehyde, acetone and propylene oxide boiling temperature are close, and propylene oxide and water, methanol etc. are respectively formed azeotropic mixture, conventional distillation
Method be difficult complete propylene oxide purifying.
As the purification process of propylene oxide, US5133839, US5262017, US5354430/1, US7285187,
Have in the patents of invention such as US8093412 and US20120077996 disclosed.It is main at present for the purifying of propylene oxide
Use C7~C20The method that straight chain and branch hydro carbons and glycols carry out extractive distillation as extractant.For example, United States Patent (USP)
It using ethylene glycol, propylene glycol, glycol monoethyl ether or diethylene glycol monomethyl ether is extractant that US3578568, which is disclosed a kind of,
Extractive distillation, the method for being allowed to separate with water, methanol, acetone and acetaldehyde are carried out to propylene oxide.It is disclosed in US3843488 pungent
The alkane of alkane etc has C to removing6Hydrocarbon impurity such as 2- methylpentane it is effective.Octane etc is disclosed in US3607669
Alkane is effective to water is removed.The hydrocarbon such as octane are disclosed in US5133839 to contained methanol, propionic aldehyde, acetone in removing propylene oxide
Equal impurity are effective.It is effective to the oxygenatedchemicals such as water impurity, propionic aldehyde, acetone are removed that glycol is disclosed in US5354430/1.
US20120077996 is in such a way that the double extractant multi-stage counter current extractions of two pure and mild normal octanes and normal octane extracting rectifying combine
Propylene oxide purification is carried out, reduces separation process energy consumption using extraction process.CN103819427A uses 4 using water as extractant
A rectifying column refines propylene oxide.CN101318944A discloses a kind of reaction, extraction rectifying by continuous operation to purify ring
The method of Ethylene Oxide.CN104109137A uses normal octane or normal heptane for extractant, carries out extracting rectifying and proposes propylene oxide.
But on the one hand above-mentioned technique is intended to the hydro carbons such as the substance such as octane outside introducing system, increase extractant cost,
Reduce product quality；On the other hand, recycling methanol is not taken into account, or the methanol of recycling cannot be recycled since concentration is not high
It uses again, causes material waste.
Summary of the invention
The technical problem to be solved by the present invention is to the prior arts due to medium outside introducing system, lead to extractant cost
Height, and recycling methanol is not taken into account, or the methanol of recycling is unable to Recycling and causes material unrestrained since concentration is not high
The problem of taking provide a kind of purification devices of new propylene oxide.Using the device purified propene oxide, do not introduce new miscellaneous
The advantages of matter has propene oxide purity high, takes into account high purity methanol recycling, and energy regenerating utilizes.
In order to solve the above technical problems, The technical solution adopted by the invention is as follows: a kind of purification devices of propylene oxide, packet
It includes:
A) the first mixer；Contact impure crude propene oxide with aqueous slkali, the first logistics is obtained；
B) the second mixer；Contact first logistics with hydrazine or hydrazine hydrate, the second logistics is obtained；
C) low-pressure distillation tower；For separating to second logistics, tower top obtains third―party logistics, and tower side line is returned
The methanol stream of receipts, tower reactor obtain heavy constituent logistics；
D) high-pressure rectification tower；For separating to the third―party logistics, tower top obtains the 4th logistics, and tower reactor obtains epoxy
Bromopropane product；4th logistics is recycled back to the low-pressure distillation tower.
In above-mentioned technical proposal, it is preferable that the crude propene oxide is after hydrogen peroxide is reacted with propylene, by recycling third
It is obtained after alkene, separating by-products.
In above-mentioned technical proposal, it is preferable that the impurity includes methanol, acetaldehyde, acetone, methyl formate and water.
In above-mentioned technical proposal, it is preferable that by weight percentage, in the crude propene oxide, the content of methanol is 5~
35%, the content of acetaldehyde is 0.01~2%, and the content of acetone is 0.01~2%, and the content of methyl formate is 0.01~2%, water
Content be 0.01~2%, the content of propylene oxide is 65~95%.
In above-mentioned technical proposal, it is preferable that the Contact Temperature of impure crude propene oxide and aqueous slkali is 30~60 DEG C；
Time of contact is greater than 30 minutes, guarantees the reaction time, reacts methyl formate completely；Contact pressure is 0.4~0.6MPaG；Control
Make pH value=7.0~7.5 of first logistics.
In above-mentioned technical proposal, it is preferable that the molar ratio of hydrazine or hydrazine hydrate and acetaldehyde is 1.0~1.5, but is not 1.0；Institute
The Contact Temperature for stating the first logistics and hydrazine or hydrazine hydrate is 30~60 DEG C；Time of contact is greater than 30 minutes；Contact pressure be 0.4~
0.6MPaG。
In above-mentioned technical proposal, it is preferable that the theoretical cam curve of the low-pressure distillation tower is 30~70 pieces, and feed entrance point is
11st~25 block of column plate above tower reactor, lateral line withdrawal function position are the 5th~15 block of column plate above tower reactor, and operation temperature is 16~32
DEG C, operating pressure is 50~100kPa, and reflux ratio is 2~7.
In above-mentioned technical proposal, it is preferable that the theoretical cam curve of the high-pressure rectification tower is 15~55 pieces, and feed entrance point is
3rd~10 block of column plate above tower reactor, operation temperature are 100~130 DEG C, 600~1400kPa of operating pressure position, reflux ratio is 2~
7。
In above-mentioned technical proposal, it is preferable that the 4th logistics is used as low-pressure distillation tower bottom reboiler heat source, is then divided into
Two strands, one returns to high-pressure rectification tower as overhead reflux, and another stock is recycled to low-pressure distillation tower further to recycle epoxy third
Alkane.
In above-mentioned technical proposal, it is preferable that the methanol concentration of the low-pressure distillation tower lateral line withdrawal function is not less than 98 weight %.
In the present invention, the pressure refers both to absolute pressure.
Hydrogen peroxide and the reaction product of propylene by Propylene recovery, to separate the reaction obtained after most by-products molten
Liquid, as the present invention used in the reaction solution containing propylene oxide, the present invention in be known as crude propene oxide.
Impurity in crude propene oxide of the present invention, mainly include methanol, acetaldehyde, acetone, methyl formate and water,
By weight percentage, the content of methanol is 5~35% to composition, and the content of acetaldehyde is 0.01~2%, and the content of acetone is 0.01
~2%, the content of methyl formate is 0.01~2%, and the content of water is 0.01~2%, and the content of propylene oxide is 65~95%.
The present invention, using the methyl formate in alkali reaction removal crude propene oxide, then second mixes again in the first mixer
Using the acetaldehyde and acetone in hydrazine reaction removal crude propene oxide in clutch, decompression-high pressure double column pressure swing rectifying column is finally used
Efficiently separating for propylene oxide and methanol is realized in operation, does not introduce new impurity, obtains purity in high-pressure rectification tower and be not less than
The product propylene of 99.95 weight % combines and is not less than the first of 98 weight % in low-pressure distillation tower recycling mass fraction
Alcohol.While effective imurity-removal, heat is provided for low pressure tower reactor reboiler preferably by high pressure overhead stream, is effectively reduced
Process energy consumption, achieves preferable technical effect.
Detailed description of the invention
Fig. 1 is apparatus of the present invention schematic diagram.
In Fig. 1, M1 is the first mixer, and M2 is the second mixer, and T1 is low-pressure distillation tower, and T2 is high-pressure rectification tower, C1
For low-pressure distillation tower top cooler, R1 is low-pressure distillation tower reactor reboiler, and R2 is high-pressure rectification tower reactor reboiler, and 1 is thick epoxy
Propane solution, 2 be aqueous slkali, and 3 be the first logistics, and 4 be hydrazine or hydrazine hydrate solution, and 5 be the second logistics, and 6 be low-pressure distillation tower top
Logistics (third―party logistics), 7 be methanol solution, and 8 be low-pressure distillation tower reactor high-boiling components, and 9 be high-pressure rectification tower top logistics (the 4th object
Stream), 10 be propylene oxide.
In Fig. 1, crude propene oxide 1 is contacted into the first mixer M1 with aqueous slkali 2, and methyl formate therein and alkali occur
Saponification resolves into methanol and sodium formate.The aqueous slkali is the aqueous solution containing sodium hydroxide, potassium hydroxide.Thick epoxy third
Alkane raw material 1 obtains the first logistics 3 after contacting with aqueous slkali 2.First logistics 3 enters the second mixer M2 and hydrazine or hydrazine hydrate
4 contacts, the carbonyls such as acetaldehyde therein, acetone, which are reduced, generates hydrazone class heavy constituent and water, generates the second logistics 5.It is described
Second logistics 5 enters low-pressure distillation tower T1, and after separation, tower top obtains the propylene oxide of higher concentration and the mixture (the of methanol
Three logistics 6), tower lateral line withdrawal function methanol 7, tower reactor obtains heavy constituent logistics 8.The third―party logistics 6 enter high-pressure rectification tower T2, point
From rear, tower top obtains propylene oxide and methanol azeotrope (the 4th logistics 9), and tower reactor obtains product propylene 10.Described 4th
Logistics 9 is used as low-pressure distillation tower bottom reboiler R1 heat source, is then divided into two strands, one returns to high-pressure rectification as overhead reflux
Tower, another stock are recycled to low-pressure distillation tower further to recycle propylene oxide.
The present invention will be further described below by way of examples.
Specific embodiment
[embodiment 1]
Using Fig. 1 shown device, the crude propene oxide group prejudice containing water, methanol, acetaldehyde, acetone, methyl formate impurity
Table 1.
Table 1
| Composition | Weight content |
| Methanol | 0.26 |
| Acetaldehyde | 0.006 |
| Acetone | 0.01 |
| Methyl formate | 0.01 |
| Water | 0.01 |
| Other | 0.004 |
| Propylene oxide | 0.7 |
The flow 10000kg/h of crude propene oxide 1 is reacted with 2 sodium hydroxide solution of logistics in the first mixer M1, formic acid
Saponification production methanol and sodium formate occur for methyl esters, and solution is reacted with 3 hydrazine solution of logistics in the second mixer M2 after reaction, will
The carbonyls such as acetaldehyde, acetone also original production hydrazone class heavy constituent and water, solution enters T1 tower top after reaction.T1 tower theory tower
Plate number is 40, and feed entrance point is the 27th block of column plate, and operating pressure control is in 60kPa, reflux ratio 4,72.4 DEG C of bottom temperature, tower
20.6 DEG C of temperature of top.7 methanol solution of logistics is extracted out from the 35th block of column plate, and tower reactor logistics 8 mainly contains sodium formate, hydrazone class heavy constituent
With the high-boiling components impurity such as water.T1 overhead stream 6 enters T2 tower top.T2 tower theoretical cam curve is 30, and feed entrance point is the 3rd piece of tower
Plate, operating pressure 700kPa, reflux ratio 4,102.6 DEG C of bottom temperature, 101.9 DEG C of tower top temperature.T2 overhead stream 9 is used as
Reboiler heat source returns to T2 tower all the way after heat exchange, enter T1 together with logistics 5 all the way to recycle propylene oxide.T2 tower reactor logistics
10 obtain the propylene oxide of high-purity.
Product propylene oxypropylene weight content has been more than 99.95%, and methanol quality content is super in methanol product
98% has been crossed, product standard has been had reached, the impurity contents such as methanol, water are as shown in table 2.In addition, T2 overhead stream 9 is T1 tower
Kettle reboiler provides 1.14MW heat, saves cold public work and hot public work 15.5% and 14.7% respectively.
Table 2
From the above it can be seen that using technical solution of the present invention, it can be with the isolated conjunction of the method for economic and energy saving
The product propylene and methanol byproduct of lattice.
[embodiment 2]
Using Fig. 1 shown device, the crude propene oxide (object containing impurity such as methanol, acetaldehyde, acetone, methyl formate and water
1) composition is shown in Table 3 to stream.
Table 3
| Composition | Weight content |
| Methanol | 0.16 |
| Acetaldehyde | 0.008 |
| Acetone | 0.007 |
| Methyl formate | 0.011 |
| Water | 0.009 |
| Propylene oxide | 0.8 |
The flow 10000kg/h of logistics 1 reacts in mixer M1 with 2 sodium hydroxide solution of logistics, methyl formate is decomposed
For methanol and sodium formate, solution is reacted with 3 hydrazine solution of logistics in mixer M2 after reaction, by carbonyls such as acetaldehyde, acetone
Also original production hydrazone class heavy constituent and water, solution enters T1 tower top after reaction.T1 tower theoretical cam curve is 50, feed entrance point the
36 blocks of column plates, operating pressure control is in 80kPa, reflux ratio 6, and 79.4 DEG C of bottom temperature, 28.1 DEG C of tower top temperature.7 first of logistics
Alcoholic solution is extracted out from the 46th block of column plate, and tower reactor logistics 8 mainly contains the high-boiling components impurity such as sodium formate, hydrazone class heavy constituent and water.T1
Overhead stream 6 enters T2 tower top.T2 tower theoretical cam curve is 40, and feed entrance point is the 5th block of column plate, and operating pressure is
1300kPa, reflux ratio 3,131.7 DEG C of bottom temperature, 129.2 DEG C of tower top temperature.T2 overhead stream 9 is used as reboiler heat source,
T2 tower is returned after heat exchange all the way, enters T1 together with logistics 5 all the way to recycle propylene oxide.T2 tower reactor logistics 10 obtains high-purity
Propylene oxide.
Product propylene oxypropylene weight content has been more than 99.95%, and methanol quality content is super in methanol product
98% has been crossed, product standard has been had reached, the impurity contents such as methanol, water are as shown in table 4.In addition, T2 overhead stream 9 is T1 tower
Kettle reboiler provides 1.15MW heat, saves cold public work and hot public work 10.0% and 9.5% respectively.
Table 4
From the above it can be seen that using technical solution of the present invention, it can be with the isolated conjunction of the method for economic and energy saving
The product propylene and methanol byproduct of lattice.
[embodiment 3]
Using Fig. 1 shown device, the crude propene oxide solution containing impurity such as methanol, acetaldehyde, acetone, methyl formate and water
(logistics 1) composition is shown in Table 5.
Table 5
| Composition | Weight content |
| Methanol | 0.07 |
| Acetaldehyde | 0.005 |
| Acetone | 0.007 |
| Methyl formate | 0.006 |
| Water | 0.01 |
| Propylene oxide | 0.9 |
The flow 10000kg/h of logistics 1 reacts in mixer M1 with 2 sodium hydroxide solution of logistics, methyl formate is decomposed
For methanol and sodium formate, solution is reacted with 3 hydrazine solution of logistics in mixer M2 after reaction, by carbonyls such as acetaldehyde, acetone
Also original production hydrazone class heavy constituent and water, solution enters T1 tower top after reaction.T1 tower theoretical cam curve is 60, feed entrance point the
45 blocks of column plates, operating pressure control is in 90kPa, reflux ratio 3, and 92.5 DEG C of bottom temperature, 31.3 DEG C of tower top temperature.7 first of logistics
Alcoholic solution is extracted out from the 54th block of column plate, and tower reactor logistics 8 mainly contains the high-boiling components impurity such as sodium formate, hydrazone class heavy constituent and water.T1
Overhead stream 6 enters T2 tower top.T2 tower theoretical cam curve is 50, and feed entrance point is the 8th block of column plate, and operating pressure is
1100kPa, reflux ratio 2,123.4 DEG C of bottom temperature, 121.2 DEG C of tower top temperature.T2 overhead stream 9 is used as reboiler heat source,
T2 tower is returned after heat exchange all the way, enters T1 together with logistics 5 all the way to recycle propylene oxide.T2 tower reactor logistics 10 obtains high-purity
Propylene oxide.
Product propylene oxypropylene weight content has been more than 99.95%, and methanol quality content is super in methanol product
98% has been crossed, product standard has been had reached, the impurity contents such as methanol, water are as shown in table 6.In addition, T2 overhead stream 9 is T1 tower
Kettle reboiler provides 1.50MW heat, saves cold public work and hot public work 16.75% and 15.36% respectively.
Table 6
From the above it can be seen that using technical solution of the present invention, it can be with the isolated conjunction of the method for economic and energy saving
The product propylene and methanol byproduct of lattice.
[comparative example 1]
As different from Example 3, T2 top gaseous phase logistics 9 is directly cooling using condenser in comparative example 1, without using
Being thermally integrated in Fig. 1；T1 tower bottom is heated using reboiler.
The flow 10000kg/h of logistics 1 reacts in mixer M1 with 2 sodium hydroxide solution of logistics, methyl formate is decomposed
For methanol and sodium formate, solution is reacted with 3 hydrazine solution of logistics in mixer M2 after reaction, by carbonyls such as acetaldehyde, acetone
Also original production hydrazone class heavy constituent and water, solution enters T1 tower top after reaction.T1 tower theoretical cam curve is 60, feed entrance point the
45 blocks of column plates, operating pressure control is in 90kPa, reflux ratio 3, and 92.5 DEG C of bottom temperature, 31.3 DEG C of tower top temperature.7 first of logistics
Alcoholic solution is extracted out from the 54th block of column plate, and tower reactor logistics 8 mainly contains the high-boiling components impurity such as sodium formate, hydrazone class heavy constituent and water.T1
Overhead stream 6 enters T2 tower top.T2 tower theoretical cam curve is 50, and feed entrance point is the 8th block of column plate, and operating pressure is
1100kPa, reflux ratio 2,123.4 DEG C of bottom temperature, 121.2 DEG C of tower top temperature.T2 overhead stream 9 is directly cold using condenser
But, T2 tower is then returned all the way, enters T1 together with logistics 5 all the way to recycle propylene oxide.T2 tower reactor logistics 10 obtains high-purity
The propylene oxide of degree.
Product propylene oxypropylene weight content has been more than 99.95%, and methanol quality content is super in methanol product
98% has been crossed, product standard has been had reached, the impurity contents such as methanol, water are as shown in table 7.
Comparative example 1 and the energy consumption comparison situation of T1 and T2 in embodiment 3 are as shown in table 8.It can be seen that with 1 phase of comparative example
Than T2 overhead stream 9 is used as T1 tower top reboiler heat source implementation heat recovery in embodiment 3, to reduce the reboiler of T1
Load, while the cooler load of T2 is saved, cold public work and hot public work 16.75% and 15.36% are reduced respectively.
Table 7
Table 8
From the above it can be seen that using technical solution of the present invention, it can be with the isolated conjunction of the method for economic and energy saving
The product propylene and methanol byproduct of lattice.
Claims (7)
1. a kind of purification devices of propylene oxide, comprising:
A) the first mixer；Contact impure crude propene oxide with aqueous slkali, the first logistics is obtained；
B) the second mixer；Contact first logistics with hydrazine or hydrazine hydrate, the second logistics is obtained；
C) low-pressure distillation tower；For separating to second logistics, tower top obtains third―party logistics, and tower side line is recycled
Methanol stream, tower reactor obtain heavy constituent logistics；
D) high-pressure rectification tower；For separating to the third―party logistics, tower top obtains the 4th logistics, and tower reactor obtains propylene oxide
Product；
The crude propene oxide is after hydrogen peroxide is reacted with propylene, to obtain after Propylene recovery, separating by-products；It is described
Impurity includes methanol, acetaldehyde, acetone, methyl formate and water；
4th logistics is used as low-pressure distillation tower bottom reboiler heat source, is then divided into two strands, one is returned as overhead reflux
High-pressure rectification tower, another stock are recycled to low-pressure distillation tower further to recycle propylene oxide.
2. the purification devices of propylene oxide according to claim 1, it is characterised in that by weight percentage, the thick epoxy
In propane, the content of methanol is 5~35%, and the content of acetaldehyde is 0.01~2%, and the content of acetone is 0.01~2%, formic acid first
The content of ester is 0.01~2%, and the content of water is 0.01~2%, and the content of propylene oxide is 65~95%.
3. the purification devices of propylene oxide according to claim 1, it is characterised in that impure crude propene oxide and alkali soluble
The Contact Temperature of liquid is 30~60 DEG C；Time of contact is greater than 30 minutes；Contact pressure is 0.4~0.6MPaG；Control described first
PH value=7.0~7.5 of logistics.
4. the purification devices of propylene oxide according to claim 1, it is characterised in that the molar ratio of hydrazine or hydrazine hydrate and acetaldehyde
It is 1.0~1.5, but is not 1.0；The Contact Temperature of first logistics and hydrazine or hydrazine hydrate is 30~60 DEG C；Time of contact is big
In 30 minutes；Contact pressure is 0.4~0.6MPaG.
5. the purification devices of propylene oxide according to claim 1, it is characterised in that the theoretical tray of the low-pressure distillation tower
Number is 30~70 pieces, and feed entrance point is the 11st~25 block of column plate above tower reactor, and lateral line withdrawal function position is the 5th~15 piece above tower reactor
Column plate, operation temperature are 16~32 DEG C, and operating pressure is 50~100kPa, and reflux ratio is 2~7.
6. the purification devices of propylene oxide according to claim 1, it is characterised in that the theoretical tray of the high-pressure rectification tower
Number is 15~55 pieces, and feed entrance point is the 3rd~10 block of column plate above tower reactor, and operation temperature is 100~130 DEG C, and operating pressure is
600~1400kPa, reflux ratio are 2~7.
7. the purification devices of propylene oxide according to claim 1, it is characterised in that the low-pressure distillation tower lateral line withdrawal function
Methanol concentration be not less than 98 weight %.
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| CN111574479A (en) * | 2020-06-12 | 2020-08-25 | 中建安装集团有限公司 | Refining process of propylene oxide |
| CN113801076A (en) * | 2020-06-16 | 2021-12-17 | 江苏怡达化学股份有限公司 | Propylene oxide rectification process |
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