CN206298529U - A kind of system of separation water and propylene glycol monomethyl ether - Google Patents
A kind of system of separation water and propylene glycol monomethyl ether Download PDFInfo
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- CN206298529U CN206298529U CN201621431405.1U CN201621431405U CN206298529U CN 206298529 U CN206298529 U CN 206298529U CN 201621431405 U CN201621431405 U CN 201621431405U CN 206298529 U CN206298529 U CN 206298529U
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- extraction
- monomethyl ether
- propylene glycol
- glycol monomethyl
- charging aperture
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Abstract
The system that the utility model provides a kind of separation water and propylene glycol monomethyl ether, including：Mixed cell, including extraction agent feeding device, the water feeder containing propylene glycol monomethyl ether, dynamic mixer and static mixer, water feeder containing propylene glycol monomethyl ether is connected with its top feed mouthful of dynamic mixer, extraction agent feeding device is respectively connected with the charging aperture of dynamic mixer side and the charging aperture of static mixer, and the discharging opening of dynamic mixer is connected with the charging aperture of static mixer；Extraction cells, are connected with the discharging opening of static mixer；De- extraction unit, is connected with the extract outlet of extraction cells.With containing the water of propylene glycol monomethyl ether can be well mixed extractant by the system, and can improve the product yield of extraction yield and propylene glycol monomethyl ether, and can the lower water containing propylene glycol monomethyl ether of concentration for the treatment of, in addition, the system architecture is simple, equipment investment is low.
Description
Technical field
The utility model belongs to chemical technology field, is related to the system of a kind of separation water and propylene glycol monomethyl ether, especially relates to
And a kind of recovery system of the accessory substance-propylene glycol monomethyl ether produced during direct oxidation of propylene production expoxy propane.
Background technology
Direct oxidation of propylene production technology is a kind of novel epoxy propane production technology, and the technical matters flow is simple, produces
Product high income, pollution-free, by-product value is high, Synthesis of Propylene Oxide just gradually traditional in surrogate.
Propylene glycol monomethyl ether is a kind of accessory substance during direct oxidation of propylene production expoxy propane, with city very high
Field value, mainly reclaims propylene glycol monomethyl ether by the way of benzene extracting rectifying at present.But, using in benzene extraction water containing ether
Water, the technology need to use substantial amounts of benzene, and extractive distillation column reflux ratio is high, steam consumption is big, high energy consumption, and propylene glycol monomethyl ether is returned
Yield is relatively low.
Currently available technology also discloses that the method for some other recovery propylene glycol monomethyl ethers, such as CN105037071 A
Disclose a kind of continuous extraction distillation and separation method of toluene-propylene glycol monomethyl ether azeotropic mixture.The method is sub- with dimethyl
Sulfone (DMSO), N, N-dimethylformamide (DMF) or the mixture constituted with arbitrary proportion, the operating condition of extractive distillation column, extraction
It is 0.5 that agent is taken with the mass ratio of charging:1-10:1, control continuous extraction rectifying tower and solvent recovery column overhead different temperatures and not
Same reflux ratio, by extractive distillation column overhead extraction toluene, solvent recovery tower overhead extraction propylene glycol monomethyl ether, the extractant of bottom of towe
Enter into extractive distillation column and recycle.
A kind of method that the A of CN 103183589 disclose separation water and propylene glycol monomethyl ether, the method includes：Use azeotropic
Agent carries out azeotropic distillation to the aqueous solution containing propylene glycol monomethyl ether, and the entrainer is cyclohexanol.Its container for being used is
Azeotrope tower.
But, the above method reclaims propylene glycol monomethyl ether and uses extracting rectifying or azeotropic distillation, and energy consumption is higher, extractant or
Entrainer usage amount is big, and the rate of recovery of propylene glycol monomethyl ether is low.
Utility model content
In view of the shortcomings of the prior art, the purpose of this utility model is to provide a kind of separation water and propane diols list first
The system of ether, the system can improve the product yield of extraction yield and propylene glycol monomethyl ether while reducing energy consumption, and can locate
The lower water containing propylene glycol monomethyl ether of reason concentration, in addition, the Solvent quantity of the system is few, steam consumption is low, equipment
Investment is low.
It is that, up to this purpose, the utility model uses following technical scheme：
A kind of system of separation water and propylene glycol monomethyl ether, the system includes：
Mixed cell, including extraction agent feeding device, the water feeder containing propylene glycol monomethyl ether, dynamic mixer and quiet
State blender, the water feeder containing propylene glycol monomethyl ether is connected with its top feed mouthful of dynamic mixer, extractant supply dress
Put and be respectively connected with the charging aperture of dynamic mixer side and the charging aperture of static mixer, the discharging opening of dynamic mixer with it is quiet
The charging aperture of state blender is connected；
Extraction cells, are connected with the discharging opening of static mixer, for the extraction of mixed material, obtain raffinate and extraction
Liquid；
De- extraction unit, is connected with the extract outlet of extraction cells, and propylene glycol monomethyl ether is reclaimed from extract.
The utility model by adjust extractant with containing propylene glycol monomethyl ether water mixed process and each device connection
Relation, can significantly improve extraction yield, and the expeditiously propylene glycol monomethyl ether in recycle-water, separately while reducing energy consumption
Outward, the system can also be used to the lower water containing propylene glycol monomethyl ether of concentration for the treatment of, and Solvent quantity is few, and steam consumption
Amount is low, and equipment investment is low.
The accessory substance-the third two that the system is produced during being particularly suited for direct oxidation of propylene production expoxy propane
The recovery of alcohol monomethyl ether.
The system also includes raffinate surge tank, and the raffinate surge tank sets charging aperture, delivery port and extractant
Outlet, charging aperture is connected with the raffinate outlet of extraction cells, and extractant outlet is connected with the charging aperture of extraction agent feeding device.
It is, in order to preferably isolate the extractant carried in raffinate waste water, to reduce the loss of extractant to set raffinate surge tank,
Make full use of the cycling extraction agent in system.
Flow control dress is set on the pipeline that the extraction agent feeding device is connected with dynamic mixer and static mixer
Put.To control the mass ratio in extractant thermally coupled flow blender and static mixer, so that containing propylene glycol monomethyl ether
Water is more abundant with the mixing of extractant, further promotes the recovery of propylene glycol monomethyl ether.
The volume control device includes regulating valve and spinner flowmeter.Those skilled in the art also can be used other streams
Amount control device.
The extractant outlet of the de- extraction unit is connected with the charging aperture of extraction agent feeding device.To recycle extraction
Agent, saves the consumption of extractant.
The extraction cells include extractor and/or extraction tower.
The bottom of the extractor and/or extraction tower sets extract outlet, extract outlet and the de- charging for extracting unit
Mouth is connected.
The de- extraction unit includes rectifying column, extractant and propane diols list first that the rectifying column can be in separating and extracting liquid
Ether.
The bottom of the rectifying column sets propylene glycol monomethyl ether outlet, and top sets extractant outlet.
Used as preferred technical scheme, the system of the separation water and propylene glycol monomethyl ether includes：Extraction agent feeding device,
Water feeder, volume control device, dynamic mixer, static mixer, extractor, raffinate containing propylene glycol monomethyl ether delay
Rush tank and rectifying column；
Water feeder containing propylene glycol monomethyl ether is connected with its top feed mouthful of dynamic mixer, extracts agent feeding device
It is respectively connected with the charging aperture of dynamic mixer side and the charging aperture of static mixer, and stream is set on connected pipeline
Amount control device, the discharging opening of dynamic mixer is connected with the charging aperture of static mixer；
The charging aperture of extractor is connected with the discharging opening of static mixer, and extractor top sets raffinate outlet, bottom
Extract outlet is set；
The charging aperture of raffinate surge tank is connected with raffinate outlet, and raffinate surge tank sets wastewater outlet and extractant
Outlet；
The charging aperture of rectifying column is exported with the extract of extractor and the extractant outlet of raffinate surge tank is respectively connected with,
The extractant outlet of rectifying column is connected with the charging aperture of extraction agent feeding device.
Compared with prior art, the beneficial effects of the utility model are：
Separation water and the system good mixing effect of propylene glycol monomethyl ether that the utility model is provided, other mixing arrangements reach
Mixed effect be only capable of reaching the 80-88% of its mixed effect；
Separation water that the utility model is provided and the system of propylene glycol monomethyl ether are mixed due to extractant and raw material to be separated
Close that effect is good, (extraction yield and the rate of recovery be only under other mixing conditions can to improve the product yield of extraction yield and propylene glycol monomethyl ether
Its 85-89%), and can the lower water containing ether of concentration for the treatment of, the concentration of propylene glycol monomethyl ether can in the water containing ether of its treatment
As little as 10%；
The separation water and the system architecture of propylene glycol monomethyl ether that the utility model is provided are simple, and equipment investment is low.
Brief description of the drawings
Fig. 1 is the connection diagram of each device in the separation water of the offer of embodiment 2 and the system of propylene glycol monomethyl ether.
Wherein：1st, agent feeding device is extracted；2, the water feeder containing propylene glycol monomethyl ether；3, dynamic mixer；4, it is quiet
State blender；5, extractor；6, raffinate surge tank；7, rectifying column.
Specific embodiment
Further illustrate the technical solution of the utility model below in conjunction with the accompanying drawings and by specific embodiment.
Embodiment 1
A kind of system of separation water and propylene glycol monomethyl ether, the system includes：
Mixed cell, including extraction agent feeding device 1, the water feeder 2 containing propylene glycol monomethyl ether, dynamic mixer 3
With static mixer 4, water feeder 2 containing propylene glycol monomethyl ether is connected with its top feed mouthful of dynamic mixer 3, extractant
Feedway 1 is respectively connected with the charging aperture of the side of dynamic mixer 3 and the charging aperture of static mixer 4, dynamic mixer 3
Discharging opening is connected with the charging aperture of static mixer 4；
Extraction cells, its charging aperture is connected with the discharging opening of static mixer 4, for the extraction of mixed material, is extracted
Extraction raffinate and extract；
De- extraction unit, its charging aperture is connected with the extract outlet of extraction cells, and propane diols list first is reclaimed from extract
Ether；
The extraction cells include extractor 5 and/or extraction tower, and the de- extraction unit includes rectifying column 7.
Flow using the system separation water and propylene glycol monomethyl ether is as follows：
(1) water containing propylene glycol monomethyl ether and extractant are mixed in dynamic mixer 3 and static mixer 4 successively
Close, obtain mixed material；
(2) mixed material is carried out into extract and separate in extractor 5, top obtains raffinate, and bottom obtains extract；
(3) extract of the bottom of extractor 5 discharge enters rectifying column 7, and through rectifying, bottom of towe obtains propylene glycol monomethyl ether product
Product.
Embodiment 2
A kind of system of separation water and propylene glycol monomethyl ether, as shown in Figure 1.
The system of the separation water and propylene glycol monomethyl ether includes：Extraction agent feeding device 1, the water containing propylene glycol monomethyl ether
Feedway 2, dynamic mixer 3, static mixer 4, extractor 5, raffinate surge tank and rectifying column 7；
Water feeder 2 containing propylene glycol monomethyl ether is connected with its top feed mouthful of dynamic mixer 3, extractant supply dress
Put 1 to be respectively connected with the charging aperture of the side of dynamic mixer 3 and the charging aperture of static mixer 4, the discharging opening of dynamic mixer 3
Charging aperture with static mixer 4 is connected；
The charging aperture of extractor 5 is connected with the discharging opening of static mixer 4, and the top of extractor 5 sets raffinate outlet, bottom
Portion sets extract outlet；
The charging aperture of raffinate surge tank 6 is connected with raffinate outlet, and raffinate surge tank 6 sets wastewater outlet and extraction
Agent is exported；
The charging aperture of rectifying column 7 is exported with the extract of extractor 5 and the extractant of raffinate surge tank 6 exports phase respectively
Even, the extractant outlet of rectifying column 7 is connected with the charging aperture of extraction agent feeding device 1.
Further, the system also includes volume control device, the extraction agent feeding device 1 and dynamic mixer 3
Volume control device is respectively provided with the pipeline being connected with static mixer 4 so that thermally coupled flow blender 3 and static mixer
Extractant in 4 maintains certain mass ratio.The volume control device includes valve and spinner flowmeter.
Flow using the system separation water and propylene glycol monomethyl ether is as follows：
(1) water containing propylene glycol monomethyl ether is mixed in dynamic mixer 3 and static mixer 4 successively with extractant,
Obtain mixed material；
(2) mixed material is carried out into extract and separate in extractor 5, raffinate is discharged from top, through raffinate surge tank 6
The residual extractant of carrying is isolated, waste water is discharged from the top of raffinate surge tank 6；
(3) extract of the bottom of extractor 5 discharge enters rectifying column 7, and the extractant isolated is recycled, and bottom of towe is obtained
Propylene glycol monomethyl ether.
The device that the utility model is provided can process the relatively low water of propylene glycol monomethyl ether concentration, using extractant extraction water
In propylene glycol monomethyl ether, extraction yield is high, and the rate of recovery of propylene glycol monomethyl ether is high, and Solvent quantity is few, the few (steam of steam consumption quantity
Used in de- extraction tower), the characteristics of equipment investment is low.
Comparative example 1
A kind of piece-rate system, in addition to static mixer 4 is replaced with into dynamic mixer 3, remaining is same as Example 2.
Using system separation water as described above and propylene glycol monomethyl ether, as a result show, under the conditions of same process, propane diols
During the rate of recovery of monomethyl ether is only the 85-90% of the propylene glycol monomethyl ether rate of recovery in embodiment 2, and extraction yield is only embodiment 2
The 85-88% of extraction yield.
Comparative example 2
A kind of piece-rate system, in addition to dynamic mixer 3 is replaced with into static mixer 4, remaining is same as Example 2.
Using system separation water as described above and propylene glycol monomethyl ether, as a result show, under the conditions of same process, propane diols
During the rate of recovery of monomethyl ether is only the 86-88% of the propylene glycol monomethyl ether rate of recovery in embodiment 2, and extraction yield is only embodiment 2
The 85-87% of extraction yield.
Comparative example 3
A kind of piece-rate system, except the order of dynamic mixer 3 and static mixer 4 is replaced, containing propylene glycol monomethyl ether
Water feeder 2 is connected with the charging of static mixer 4, the discharging opening of static mixer 4 and the charging aperture phase of dynamic mixer 3
Even, the discharging opening of dynamic mixer 3 is connected outer with the charging aperture of extractor 5, and remaining is same as Example 2.
Using system separation water as described above and propylene glycol monomethyl ether, as a result show, under the conditions of same process, propane diols
During the rate of recovery of monomethyl ether is only the 87-89% of the propylene glycol monomethyl ether rate of recovery in embodiment 2, and extraction yield is only embodiment 2
The 87-88% of extraction yield.
Applicant's statement, the foregoing is only specific embodiment of the present utility model, but protection model of the present utility model
Enclose and be not limited thereto, person of ordinary skill in the field is it will be clearly understood that any belong to those skilled in the art and exist
In the technical scope that the utility model is disclosed, the change or replacement that can be readily occurred in all fall within protection domain of the present utility model
Within the scope of disclosure.
Claims (10)
1. the system of a kind of separation water and propylene glycol monomethyl ether, it is characterised in that the system includes：
Mixed cell, including extraction agent feeding device (1), the water feeder (2) containing propylene glycol monomethyl ether, dynamic mixer
(3) and static mixer (4), its top feed mouthful phase of the water feeder (2) containing propylene glycol monomethyl ether and dynamic mixer (3)
Even, extraction agent feeding device (1) distinguishes phase with the charging aperture of dynamic mixer (3) side and the charging aperture of static mixer (4)
Even, the discharging opening of dynamic mixer (3) is connected with the charging aperture of static mixer (4)；
Extraction cells, the discharging opening with static mixer (4) is connected, and for the extraction of mixed material, obtains raffinate and extraction
Liquid；
De- extraction unit, is connected with the extract outlet of extraction cells, and propylene glycol monomethyl ether is reclaimed from extract.
2. system according to claim 1, it is characterised in that the system also includes raffinate surge tank (6), the extraction
Extraction raffinate surge tank (6) sets the outlet of charging aperture, delivery port and extractant, and charging aperture is connected with the raffinate outlet of extraction cells,
Extractant is exported and is connected with the charging aperture of extraction agent feeding device (1).
3. system according to claim 1 and 2, it is characterised in that the extraction agent feeding device (1) and dynamic mixer
(3) volume control device is set on the pipeline being connected with static mixer (4).
4. system according to claim 3, it is characterised in that the volume control device includes regulating valve and spinner
Meter.
5. system according to claim 1 and 2, it is characterised in that the extractant outlet of the de- extraction unit and extractant
The charging aperture of feedway (1) is connected.
6. system according to claim 1 and 2, it is characterised in that the extraction cells include extractor (5) and/or extraction
Take tower.
7. system according to claim 6, it is characterised in that the bottom of the extractor (5) and/or extraction tower sets extraction
Liquid outlet is taken, extract outlet is connected with the charging aperture of de- extraction unit.
8. system according to claim 1 and 2, it is characterised in that the de- extraction unit includes rectifying column (7).
9. system according to claim 8, it is characterised in that the bottom of the rectifying column (7) sets propylene glycol monomethyl ether
Outlet, top sets extractant outlet.
10. system according to claim 1 and 2, it is characterised in that the system includes：Extraction agent feeding device (1),
Water feeder (2), volume control device containing propylene glycol monomethyl ether, dynamic mixer (3), static mixer (4), extractor
(5), raffinate surge tank (6) and rectifying column (7)；
Water feeder (2) containing propylene glycol monomethyl ether is connected with its top feed mouthful of dynamic mixer (3), extractant supply dress
(1) is put to be respectively connected with the charging aperture of dynamic mixer (3) side and the charging aperture of static mixer (4), and be connected
Volume control device is set on pipeline, and the discharging opening of dynamic mixer (3) is connected with the charging aperture of static mixer (4)；
The charging aperture of extractor (5) is connected with the discharging opening of static mixer (4), and extractor (5) top sets raffinate outlet,
Bottom sets extract outlet；
The charging aperture of raffinate surge tank (6) is connected with raffinate outlet, and raffinate surge tank (6) sets wastewater outlet and extraction
Agent is exported；
The charging aperture of rectifying column (7) and the extract outlet of extractor (5) and the extractant outlet difference of raffinate surge tank (6)
It is connected, the extractant outlet of rectifying column (7) is connected with the charging aperture of extraction agent feeding device (1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621431405.1U CN206298529U (en) | 2016-12-23 | 2016-12-23 | A kind of system of separation water and propylene glycol monomethyl ether |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621431405.1U CN206298529U (en) | 2016-12-23 | 2016-12-23 | A kind of system of separation water and propylene glycol monomethyl ether |
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| CN206298529U true CN206298529U (en) | 2017-07-04 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110857226A (en) * | 2018-08-23 | 2020-03-03 | 中国石油化工股份有限公司 | Combined method for treating wastewater from propylene oxide production and desalting crude oil |
| CN110857234A (en) * | 2018-08-23 | 2020-03-03 | 中国石油化工股份有限公司 | Method for treating wastewater from propylene oxide production |
| CN113754522A (en) * | 2021-10-12 | 2021-12-07 | 华东理工大学 | Separation process of water-propylene glycol monomethyl ether-propylene glycol ternary system |
-
2016
- 2016-12-23 CN CN201621431405.1U patent/CN206298529U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110857226A (en) * | 2018-08-23 | 2020-03-03 | 中国石油化工股份有限公司 | Combined method for treating wastewater from propylene oxide production and desalting crude oil |
| CN110857234A (en) * | 2018-08-23 | 2020-03-03 | 中国石油化工股份有限公司 | Method for treating wastewater from propylene oxide production |
| CN113754522A (en) * | 2021-10-12 | 2021-12-07 | 华东理工大学 | Separation process of water-propylene glycol monomethyl ether-propylene glycol ternary system |
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