CN106397364A - Purifying apparatus for epoxypropane - Google Patents
Purifying apparatus for epoxypropane Download PDFInfo
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- CN106397364A CN106397364A CN201510468102.0A CN201510468102A CN106397364A CN 106397364 A CN106397364 A CN 106397364A CN 201510468102 A CN201510468102 A CN 201510468102A CN 106397364 A CN106397364 A CN 106397364A
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- expoxy propane
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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
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- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Epoxy Compounds (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to a purifying apparatus for epoxypropane. The purifying apparatus mainly overcomes the problems of high cost of an extractant due to introduction of a medium out of a system and incapability of recovery of methanol or material waste resulting from incapable recycling of recovered methanol due to low concentration of recovered methanol in the prior art. The purifying apparatus comprises a) a first mixer used for allowing crude epoxypropane containing impurities to contact with aqueous alkali so as to obtain first material flow; b) a second mixer used for allowing the first material flow to contact with hydrazine hydrate so as to obtain second material flow; c) a low-pressure rectifying tower used for separating the second material flow, wherein third material flow is obtained at the top of the rectifying tower, recovered methanol material flow is obtained at the side line of the tower, and a heavy-component material flow is obtained at the bottom of the tower; and d) a high-pressure rectifying tower used for separating the third material flow, wherein fourth material flow is obtained at the top of the rectifying tower and cyclically returns to the low-pressure rectifying tower, and an epoxypropane product is obtained at the bottom of the tower. Thus, the purifying apparatus overcomes the above problems and can be used for industrial purification of epoxypropane.
Description
Technical field
The present invention relates to a kind of purification devices of expoxy propane, the direct oxygen of more particularly, to a kind of hydrogen peroxide
It is thick containing impurity such as water, methanol, acetaldehyde, acetone, methyl formates that change method (HPPO) produces
Oxide purification device.
Background technology
Expoxy propane is important organic compound raw material, mainly for the production of polyether polyol, third
Glycol and all kinds of nonionic surfactant etc., wherein polyether polyol are to produce polyurethane foam, guarantor
The important source material of adiabator, elastomer, adhesive and coating etc., all kinds of nonionic surfactant
It is used widely in industries such as oil, chemical industry, pesticide, weaving, daily use chemicals.But only have relatively
Highly purified expoxy propane can be used for manufacturing polyvalent alcohol, therefore thick to the expoxy propane of synthesis
Product can be applied to prepare polyvalent alcohol after carrying out purification processes.And there is polymerization institute in expoxy propane
The condition wanted, does not require nothing more than propene oxide purity and reaches 99.95 weight %, to water impurity, aldehyde, non-
The content of volatile matters has strict demand.
Hydrogen peroxide direct oxidation method (HPPO method) is in the presence of molecular sieve catalyst, in first
Using the method for hydrogen peroxide direct oxidation propylene synthesizing epoxypropane in alcoholic solution.Through Propylene recovery,
The crude propene oxide obtaining after separating by-products, still contain methanol, acetaldehyde, acetone, methyl formate and
The impurity such as water.In order to obtain meeting the high-purity expoxy propane that polymerization requires it is necessary to by expoxy propane
The impurity containing is separated off.Because methyl formate and expoxy propane relative volatility are close to 1, second
Aldehyde, acetone and expoxy propane boiling temperature are close, and expoxy propane and water, methanol etc. are respectively formed azeotropic mixture
The features such as, the method for conventional distillation has been difficult to complete the purification of expoxy propane.
As the purification process of expoxy propane, US5133839, US5262017, US5354430/1,
All have disclosed in the patents of invention such as US7285187, US8093412 and US20120077996.Just
For the purification of expoxy propane, it is currently mainly used C7～C20Straight chain and side chain hydro carbons and glycolss are made
The method carrying out extractive distillation for extractant.For example, United States Patent (USP) US3578568 discloses one kind
The use of ethylene glycol, propylene glycol, glycol monoethyl ether or diethylene glycol monomethyl ether is extractant, to ring
Ethylene Oxide carries out extractive distillation, is allowed to and water, methanol, acetone and the detached method of acetaldehyde.
The alkane disclosing octane etc in US3843488 has C to removing6Hydrocarbon impurity such as 2- methylpent
Alkane is effective.The alkane disclosing octane etc in US3607669 is effective to removing water.US5133839
In disclose the hydrocarbon such as octane to remove expoxy propane in the impurity such as contained methanol, propionic aldehyde, acetone effective.
Glycol is disclosed effective to removing the oxygenatedchemicalss such as water impurity, propionic aldehyde, acetone in US5354430/1.
US20120077996 adopts glycol and the double extractant multi-stage counter current extraction of normal octane and normal octane extraction
The mode that rectification combines carries out expoxy propane purification, reduces separation process energy consumption using extraction process.
CN103819427A, with water as extractant, refines expoxy propane using 4 rectifying columns.
CN101318944A discloses a kind of reaction, extraction rectification by continuous operation and purifies epoxy third
The method of alkane.It is extractant that CN104109137A adopts normal octane or normal heptane, carries out extracting rectifying
Expoxy propane is proposed.
But, above-mentioned technique one side is intended to the hydro carbons such as the material such as octane outside introducing system, increased
Extractant cost, reduces product quality；On the other hand, do not take into account recovery methanol, or reclaim
Methanol be unable to Recycling because concentration is not high, cause material waste.
Content of the invention
The technical problem to be solved is prior art due to the outer medium of introducing system, leads to extract
Take agent high cost, and do not take into account recovery methanol, or the methanol reclaiming is because concentration is not high not
Can Recycling and lead to the problem of material waste, a kind of purification devices of new expoxy propane are provided.
Using this device purified propene oxide, do not introduce new impurity, there is propene oxide purity height, take into account
High purity methanol reclaims, the advantage that energy regenerating utilizes.
For solving above-mentioned technical problem, the technical solution used in the present invention is as follows：A kind of expoxy propane
Purification devices, including：
A) the first blender；Crude propene oxide in order to make impure is contacted with aqueous slkali, obtains
One logistics；
B) the second blender；In order to make described first logistics contact with hydrazine or hydrazine hydrate, obtain second
Logistics；
C) low-pressure distillation tower；For carrying out to described second logistics separating, tower top obtains third-party logistics,
The methanol stream that tower side line is recycled, tower reactor obtains heavy constituent logistics；
D) high-pressure rectification tower；For carrying out to described third-party logistics separating, tower top obtains the 4th logistics,
Tower reactor obtains product propylene；Described 4th logistics loops back described low-pressure distillation tower.
It is preferable that after described crude propene oxide reacted with propylene for hydrogen peroxide in technique scheme,
Obtain after Propylene recovery, separating by-products.
It is preferable that described impurity comprises methanol, acetaldehyde, acetone, formic acid first in technique scheme
Ester and water.
In technique scheme it is preferable that by weight percentage, in described crude propene oxide, first
The content of alcohol is 5～35%, and the content of acetaldehyde is 0.01～2%, and the content of acetone is 0.01～2%, first
The content of sour methyl ester is 0.01～2%, and the content of water is 0.01～2%, and the content of expoxy propane is
65～95%.
It is preferable that the Contact Temperature of impure crude propene oxide and aqueous slkali in technique scheme
For 30～60 DEG C；It is more than 30 minutes time of contact it is ensured that the response time, make methyl formate completely anti-
Should；Contact pressure is 0.4～0.6MPaG；Control pH value=7.0～7.5 of described first logistics.
It is preferable that hydrazine or hydrazine hydrate are 1.0～1.5 with the mol ratio of acetaldehyde in technique scheme,
But it is not 1.0；Described first logistics is 30～60 DEG C with the Contact Temperature of hydrazine or hydrazine hydrate；During contact
Between be more than 30 minutes；Contact pressure is 0.4～0.6MPaG.
It is preferable that the theoretical cam curve of described low-pressure distillation tower is 30～70 pieces in technique scheme,
Feed entrance point is the 11st～25 block of column plate above tower reactor, and lateral line withdrawal function position is the 5th～15 above tower reactor
Block column plate, operation temperature is 16～32 DEG C, and operating pressure is 50～100kPa, and reflux ratio is 2～7.
It is preferable that the theoretical cam curve of described high-pressure rectification tower is 15～55 pieces in technique scheme,
Feed entrance point is the 3rd～10 block of column plate above tower reactor, and operation temperature is 100～130 DEG C, operating pressure
Position 600～1400kPa, reflux ratio is 2～7.
It is preferable that described 4th logistics is used as low-pressure distillation bottom of towe reboiler heat in technique scheme
Source, is then divided into two strands, and one returns high-pressure rectification tower as overhead reflux, and another stock is recycled to low
Pressure rectifying column is to reclaim expoxy propane further.
It is preferable that the methanol concentration of described low-pressure distillation tower lateral line withdrawal function is not low in technique scheme
In 98 weight %.
In the present invention, described pressure refers both to absolute pressure.
The product of hydrogen peroxide and propylene through Propylene recovery, separate after most by-products
The reaction solution containing expoxy propane used in the reaction solution arriving, the as present invention, the present invention
In referred to as crude propene oxide.
Impurity in crude propene oxide of the present invention, mainly includes methanol, acetaldehyde, acetone, first
Sour methyl ester and water, by weight percentage, the content of methanol is 5～35% to its composition, the content of acetaldehyde
For 0.01～2%, the content of acetone is 0.01～2%, and the content of methyl formate is 0.01～2%, water
Content is 0.01～2%, and the content of expoxy propane is 65～95%.
The present invention adopts alkali reaction to remove the methyl formate in crude propene oxide, so in the first blender
Adopt hydrazine reaction to remove acetaldehyde and acetone in crude propene oxide afterwards again in second blender, finally adopt
Efficiently separating of expoxy propane and methanol is realized in the operation of decompression-high pressure double column pressure swing rectifying column, does not introduce
New impurity, obtains, in high-pressure rectification tower, the product propylene that purity is not less than 99.95 weight %,
Take into account simultaneously and reclaim, in low-pressure distillation tower, the methanol that mass fraction is not less than 98 weight %.Effectively de-
Deimpurity likewise it is preferred that using high pressure overhead stream be low pressure tower reactor reboiler provide heat, effectively
Reduce process energy consumption, achieve preferable technique effect.
Brief description
Fig. 1 is apparatus of the present invention sketch.
In Fig. 1, M1 is the first blender, and M2 is the second blender, and T1 is low-pressure distillation tower,
T2 is high-pressure rectification tower, and C1 is low-pressure distillation tower top cooler, and R1 boils for low-pressure distillation tower reactor again
Device, R2 is high-pressure rectification tower reactor reboiler, and 1 is crude propene oxide solution, and 2 is aqueous slkali, and 3 are
First logistics, 4 is hydrazine or hydrazine hydrate solution, and 5 is the second logistics, and 6 is low-pressure distillation tower top logistics
(third-party logistics), 7 is methanol solution, and 8 is low-pressure distillation tower reactor high-boiling components, and 9 is high-pressure rectification
Overhead stream (the 4th logistics), 10 is expoxy propane.
In Fig. 1, crude propene oxide 1 is entered the first blender M1 and is contacted with aqueous slkali 2, therein
There is saponification with alkali in methyl formate, resolve into methanol and sodium formate.Described aqueous slkali is containing hydrogen-oxygen
Change sodium, the aqueous solution of potassium hydroxide.Crude propene oxide raw material 1 obtains first after contacting with aqueous slkali 2
Logistics 3.Described first logistics 3 is entered the second blender M2 and is contacted with hydrazine or hydrazine hydrate 4, wherein
Acetaldehyde, the carbonyl compound such as acetone be reduced generation hydrazone class heavy constituent and water, generate the second logistics 5.
Described second logistics 5 enters low-pressure distillation tower T1, and after separating, tower top obtains the epoxy of higher concentration
The mixture (third-party logistics 6) of propane and methanol, tower lateral line withdrawal function methanol 7, tower reactor is recombinated
Divide logistics 8.Described third-party logistics 6 enter high-pressure rectification tower T2, and after separating, tower top obtains epoxy third
Alkane and methanol azeotrope (the 4th logistics 9), tower reactor obtains product propylene 10.Described 4th thing
Stream 9 is used as low-pressure distillation bottom of towe reboiler R1 thermal source, is then divided into two strands, one returns as tower top
Stream returns high-pressure rectification tower, and another stock is recycled to low-pressure distillation tower to reclaim expoxy propane further.
Below by embodiment, the invention will be further elaborated.
Specific embodiment
【Embodiment 1】
Using Fig. 1 shown device, containing water, methanol, acetaldehyde, acetone, methyl formate impurity thick
Expoxy propane composition is shown in 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 |
| Expoxy propane | 0.7 |
The flow 10000kg/h of crude propene oxide 1, is mixed first with logistics 2 sodium hydroxide solution
Device M1 reacts, and methyl formate occurs saponification to produce methanol and sodium formate, solution and thing after reaction
Flow 3 hydrazine solutions to react in the second blender M2, by the also original production of the carbonyl compounds such as acetaldehyde, acetone
Hydrazone class heavy constituent and water, after reaction, solution enters T1 tower top.T1 tower theoretical cam curve is 40,
Feed entrance point is the 27th block of column plate, and operating pressure controls in 60kPa, and reflux ratio is 4, bottom temperature
72.4 DEG C, 20.6 DEG C of tower top temperature.Logistics 7 methanol solution is extracted out from the 35th block of column plate, tower reactor thing
Stream 8 mainly contains the high-boiling components impurity such as sodium formate, hydrazone class heavy constituent and water.T1 overhead stream 6 enters
Enter T2 tower top.T2 tower theoretical cam curve is 30, and feed entrance point is the 3rd block of column plate, operation pressure
Power is 700kPa, and reflux ratio is 4,102.6 DEG C of bottom temperature, 101.9 DEG C of tower top temperature.T2 tower
Top logistics 9 is used as reboiler thermal source, and after heat exchange, a road returns T2 tower, is gone forward side by side with logistics 5 one in a road
Enter T1 to reclaim expoxy propane.T2 tower reactor logistics 10 obtains highly purified expoxy propane.
Product propylene oxypropylene weight content has exceeded 99.95%, methanol in methanol product
Mass content has exceeded 98%, has all reached product standard, the impurity content such as methanol, water such as table 2
Shown.Additionally, T2 overhead stream 9 provides 1.14MW heat for T1 tower reactor reboiler, save respectively
Save cold public work and hot public work 15.5% and 14.7%.
Table 2
From the above it can be seen that adopting technical scheme, can be with the method for economic and energy saving
Separate and obtain qualified product propylene and methanol side-product.
【Embodiment 2】
Using Fig. 1 shown device, containing impurity such as methanol, acetaldehyde, acetone, methyl formate and water
Crude propene oxide (logistics 1) composition is shown in Table 3.
Table 3
| Composition | Weight content |
| Methanol | 0.16 |
| Acetaldehyde | 0.008 |
| Acetone | 0.007 |
| Methyl formate | 0.011 |
| Water | 0.009 |
| Expoxy propane | 0.8 |
The flow 10000kg/h of logistics 1, is reacted in blender M1 with logistics 2 sodium hydroxide solution,
Methyl formate is decomposed into methanol and sodium formate, after reaction, solution and logistics 3 hydrazine solution are in blender
M2 reacts, by the carbonyl compounds such as acetaldehyde, acetone also original production hydrazone class heavy constituent and water, after reaction
Solution enters T1 tower top.T1 tower theoretical cam curve is 50, and feed entrance point is the 36th block of column plate,
Operating pressure controls in 80kPa, and reflux ratio is 6,79.4 DEG C of bottom temperature, 28.1 DEG C of tower top temperature.
Logistics 7 methanol solution is extracted out from the 46th block of column plate, and tower reactor logistics 8 mainly contains sodium formate, hydrazone class
The high-boiling components impurity such as heavy constituent and water.T1 overhead stream 6 enters T2 tower top.T2 tower theory tower
Plate number is 40, and feed entrance point is the 5th block of column plate, and operating pressure is 1300kPa, and reflux ratio is 3,
131.7 DEG C of bottom temperature, 129.2 DEG C of tower top temperature.T2 overhead stream 9 is used as reboiler thermal source,
After heat exchange, a road returns T2 tower, and a road and logistics 5 enter T1 in the lump to reclaim expoxy propane.T2
Tower reactor logistics 10 obtains highly purified expoxy propane.
Product propylene oxypropylene weight content has exceeded 99.95%, methanol in methanol product
Mass content has exceeded 98%, has all reached product standard, the impurity content such as methanol, water such as table 4
Shown.Additionally, T2 overhead stream 9 provides 1.15MW heat for T1 tower reactor reboiler, save respectively
Save cold public work and hot public work 10.0% and 9.5%.
Table 4
From the above it can be seen that adopting technical scheme, can be with the method for economic and energy saving
Separate and obtain qualified product propylene and methanol side-product.
【Embodiment 3】
Using Fig. 1 shown device, containing impurity such as methanol, acetaldehyde, acetone, methyl formate and water
Crude propene oxide solution (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 |
| Expoxy propane | 0.9 |
The flow 10000kg/h of logistics 1, is reacted in blender M1 with logistics 2 sodium hydroxide solution,
Methyl formate is decomposed into methanol and sodium formate, after reaction, solution and logistics 3 hydrazine solution are in blender
M2 reacts, by the carbonyl compounds such as acetaldehyde, acetone also original production hydrazone class heavy constituent and water, after reaction
Solution enters T1 tower top.T1 tower theoretical cam curve is 60, and feed entrance point is the 45th block of column plate,
Operating pressure controls in 90kPa, and reflux ratio is 3,92.5 DEG C of bottom temperature, 31.3 DEG C of tower top temperature.
Logistics 7 methanol solution is extracted out from the 54th block of column plate, and tower reactor logistics 8 mainly contains sodium formate, hydrazone class
The high-boiling components impurity such as heavy constituent and water.T1 overhead stream 6 enters T2 tower top.T2 tower theory tower
Plate number is 50, and feed entrance point is the 8th block of column plate, and operating pressure is 1100kPa, and reflux ratio is 2,
123.4 DEG C of bottom temperature, 121.2 DEG C of tower top temperature.T2 overhead stream 9 is used as reboiler thermal source,
After heat exchange, a road returns T2 tower, and a road and logistics 5 enter T1 in the lump to reclaim expoxy propane.T2
Tower reactor logistics 10 obtains highly purified expoxy propane.
Product propylene oxypropylene weight content has exceeded 99.95%, methanol in methanol product
Mass content has exceeded 98%, has all reached product standard, the impurity content such as methanol, water such as table 6
Shown.Additionally, T2 overhead stream 9 provides 1.50MW heat for T1 tower reactor reboiler, save respectively
Save cold public work and hot public work 16.75% and 15.36%.
Table 6
From the above it can be seen that adopting technical scheme, can be with the method for economic and energy saving
Separate and obtain qualified product propylene and methanol side-product.
【Comparative example 1】
As different from Example 3, in comparative example 1, T2 top gaseous phase logistics 9 adopts condenser straight
Connect cooling, and not using being thermally integrated in Fig. 1；T1 bottom of towe adopts reboiler to heat.
The flow 10000kg/h of logistics 1, is reacted in blender M1 with logistics 2 sodium hydroxide solution,
Methyl formate is decomposed into methanol and sodium formate, after reaction, solution and logistics 3 hydrazine solution are in blender
M2 reacts, by the carbonyl compounds such as acetaldehyde, acetone also original production hydrazone class heavy constituent and water, after reaction
Solution enters T1 tower top.T1 tower theoretical cam curve is 60, and feed entrance point is the 45th block of column plate,
Operating pressure controls in 90kPa, and reflux ratio is 3,92.5 DEG C of bottom temperature, 31.3 DEG C of tower top temperature.
Logistics 7 methanol solution is extracted out from the 54th block of column plate, and tower reactor logistics 8 mainly contains sodium formate, hydrazone class
The high-boiling components impurity such as heavy constituent and water.T1 overhead stream 6 enters T2 tower top.T2 tower theory tower
Plate number is 50, and feed entrance point is the 8th block of column plate, and operating pressure is 1100kPa, and reflux ratio is 2,
123.4 DEG C of bottom temperature, 121.2 DEG C of tower top temperature.T2 overhead stream 9 adopts condenser directly cold
But, then a road returns T2 tower, and a road and logistics 5 enter T1 in the lump to reclaim expoxy propane.
T2 tower reactor logistics 10 obtains highly purified expoxy propane.
Product propylene oxypropylene weight content has exceeded 99.95%, methanol in methanol product
Mass content has exceeded 98%, has all reached product standard, the impurity content such as methanol, water such as table 7
Shown.
Comparative example 1 is as shown in table 8 with the energy consumption comparison situation of T1 and T2 in embodiment 3.Thus
It can be seen that, compared with comparative example 1, in embodiment 3, T2 overhead stream 9 is used as T1 tower top reboiler
Thermal source implements heat recovery, thus decreasing the reboiler of T1, saves the cold of T2 simultaneously
But device load, reduces cold public work and hot public work 16.75% and 15.36% respectively.
Table 7
Table 8
From the above it can be seen that adopting technical scheme, can be with the method for economic and energy saving
Separate and obtain qualified product propylene and methanol side-product.
Claims (10)
1. a kind of purification devices of expoxy propane, including：
A) the first blender；Crude propene oxide in order to make impure is contacted with aqueous slkali, obtains
One logistics；
B) the second blender；In order to make described first logistics contact with hydrazine or hydrazine hydrate, obtain second
Logistics；
C) low-pressure distillation tower；For carrying out to described second logistics separating, tower top obtains third-party logistics,
The methanol stream that tower side line is recycled, tower reactor obtains heavy constituent logistics；
D) high-pressure rectification tower；For carrying out to described third-party logistics separating, tower top obtains the 4th logistics,
Tower reactor obtains product propylene；Described 4th logistics loops back described low-pressure distillation tower.
2. according to claim 1 the purification devices of expoxy propane it is characterised in that described thick ring
After Ethylene Oxide is reacted with propylene for hydrogen peroxide, obtain after Propylene recovery, separating by-products.
3. according to claim 1 the purification process of expoxy propane it is characterised in that described impurity
Comprise methanol, acetaldehyde, acetone, methyl formate and water.
4. according to claim 3 the purification devices of expoxy propane it is characterised in that with weight hundred
Divide than meter, in described crude propene oxide, the content of methanol is 5～35%, and the content of acetaldehyde is 0.01～2%,
The content of acetone is 0.01～2%, and the content of methyl formate is 0.01～2%, and the content of water is 0.01～2%,
The content of expoxy propane is 65～95%.
5. according to claim 1 the purification devices of expoxy propane it is characterised in that impure
Crude propene oxide is 30～60 DEG C with the Contact Temperature of aqueous slkali；Time of contact is more than 30 minutes；Connect
Touch pressure is 0.4～0.6MPaG；Control pH value=7.0～7.5 of described first logistics.
6. according to claim 1 the purification devices of expoxy propane it is characterised in that hydrazine or hydration
Hydrazine is 1.0～1.5 with the mol ratio of acetaldehyde, but is not 1.0；Described first logistics and hydrazine or hydrazine hydrate
Contact Temperature is 30～60 DEG C；Time of contact is more than 30 minutes；Contact pressure is 0.4～0.6MPaG.
7. according to claim 1 the purification devices of expoxy propane it is characterised in that described low pressure
The theoretical cam curve of rectifying column is 30～70 pieces, and feed entrance point is the 11st～25 block of column plate above tower reactor,
Lateral line withdrawal function position is the 5th～15 block of column plate above tower reactor, and operation temperature is 16～32 DEG C, operation pressure
Power is 50～100kPa, and reflux ratio is 2～7.
8. according to claim 1 the purification devices of expoxy propane it is characterised in that described high pressure
The theoretical cam curve of rectifying column is 15～55 pieces, and feed entrance point is the 3rd～10 block of column plate above tower reactor,
Operation temperature is 100～130 DEG C, operating pressure position 600～1400kPa, and reflux ratio is 2～7.
9. according to claim 1 the purification devices of expoxy propane it is characterised in that the described 4th
Logistics is used as low-pressure distillation bottom of towe reboiler thermal source, is then divided into two strands, one returns as overhead reflux
Return high-pressure rectification tower, another stock is recycled to low-pressure distillation tower to reclaim expoxy propane further.
10. oxide purification device according to claim 1 is it is characterised in that described low pressure
The methanol concentration of rectifying column lateral line withdrawal function is not less than 98 weight %.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109608320A (en) * | 2019-01-09 | 2019-04-12 | 天津精分科技发展有限公司 | A kind of separation method of acetone and water mixed solvent |
| 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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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1714087A (en) * | 2002-11-26 | 2005-12-28 | 德古萨股份公司 | Process for the purification of crude propene oxide |
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- 2015-08-03 CN CN201510468102.0A patent/CN106397364B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1714087A (en) * | 2002-11-26 | 2005-12-28 | 德古萨股份公司 | Process for the purification of crude propene oxide |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109608320A (en) * | 2019-01-09 | 2019-04-12 | 天津精分科技发展有限公司 | A kind of separation method of acetone and water mixed solvent |
| 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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