CN206494868U - A kind of three-tower differential pressure coupling rectification system of low carbon mixed alcohol separation - Google Patents
A kind of three-tower differential pressure coupling rectification system of low carbon mixed alcohol separation Download PDFInfo
- Publication number
- CN206494868U CN206494868U CN201720104741.3U CN201720104741U CN206494868U CN 206494868 U CN206494868 U CN 206494868U CN 201720104741 U CN201720104741 U CN 201720104741U CN 206494868 U CN206494868 U CN 206494868U
- Authority
- CN
- China
- Prior art keywords
- tower
- outlet
- ethanol propanol
- dehydrating
- methanol
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a kind of three-tower differential pressure coupling rectification system of low carbon mixed alcohol separation.The three-tower differential pressure coupling rectification system includes dehydrating tower, methanol column and the ethanol propanol tower being sequentially communicated, and further comprises：Dehydrating tower after-condenser is provided with the path of dehydrating tower primary condenser, dehydration column overhead steam (vapor) outlet and dehydrating tower, the outlet of the first gas phase mixture is connected with the tower reactor of methanol column, and the outlet of the first liquid phase mixture is connected with ethanol propanol tower；And ethanol propanol tower primary condenser, ethanol propanol overhead vapours exports and is provided with ethanol propanol tower after-condenser on the path with ethanol propanol tower, the outlet of second gas phase mixture is connected with the tower reactor of methanol column, and second liquid phase mixture outlet is connected with ethanol propanol tower.The three-tower differential pressure coupling rectification system separated using low carbon mixed alcohol of the present utility model, is greatly reduced production cost and energy consumption, in theory Finestill energy-saving nearly 30%.
Description
Technical field
The utility model is related to mixed alcohol separation technology field, three separated in particular to a kind of low carbon mixed alcohol
Tower differential pressure coupling rectification system.
Background technology
Low carbon mixed alcohol refers to the mixed alcohol formed by C1-C6 alcohols, its mainly by coal based synthetic gas synthesize it is thick
Mixed alcohol carries out what is formed after dewater treatment.Low carbon mixed alcohol can replace methyl tertiary butyl ether(MTBE) as gasoline additive, simultaneously
Itself it is also a kind of good clean fuel, fuel can be used as instead of gasoline.Low carbon mixed alcohol is separated, can be obtained
To the senior chemical industry alcohol such as first, second, third, fourth, amylalcohol, these simple products are important chemical intermediates, with higher economy
Value, therefore, the research for carrying out low carbon mixed alcohol separating technology are significant.
However, due in low carbon mixed alcohol alcohol component it is more, when carrying out rectifying separation using traditional distillation system, because
Theoretical plate is more, and reflux ratio is big, causes energy consumption very big, and wherein energy consumption highest workshop section is methanol section.It is anxious in order to solve the above problems
A kind of new separating technology is needed, to reduce energy consumption.
Utility model content
The utility model aims to provide a kind of three-tower differential pressure coupling rectification system of low carbon mixed alcohol separation, existing to solve
Energy consumption big technical problem when low carbon mixed alcohol rectifying is separated in technology.
To achieve these goals, separated according to one side of the present utility model there is provided a kind of low carbon mixed alcohol
Three-tower differential pressure coupling rectification system.The three-tower differential pressure coupling rectification system includes dehydrating tower, methanol column and the ethanol being sequentially communicated
Propyl alcohol tower, further comprises：Dehydrating tower primary condenser, is provided with dehydration column overhead steam inlet, dehydration column overhead steam and goes out
Mouth and methanol column tower bottoms first entrance, the outlet of the first gas phase mixture and the outlet of the first liquid phase mixture, dehydration column overhead
Dehydrating tower after-condenser, the outlet of the first gas phase mixture and the tower of methanol column are provided with the path of steam (vapor) outlet and dehydrating tower
Kettle is connected, and the outlet of the first liquid phase mixture is connected with ethanol propanol tower；And ethanol propanol tower primary condenser, it is provided with
Ethanol propanol overhead vapours entrance, the outlet of ethanol propanol overhead vapours and methanol column tower bottoms second entrance, the second gas phase are mixed
Compound is exported and second liquid phase mixture outlet, and the outlet of ethanol propanol overhead vapours on the path of ethanol propanol tower with being provided with second
Alcohol propyl alcohol tower after-condenser, the second gas phase mixture outlet is connected with the tower reactor of methanol column, second liquid phase mixture outlet
It is connected with ethanol propanol tower.
Further, three-tower differential pressure coupling rectification system, in addition to：Dehydrating tower tower bottom reboiler, the dehydration with dehydrating tower
Tower tower bottoms is exported and dehydrating tower boils kettle liquid entrance and is connected again, methanol column bottom of towe auxiliary reboiler, the methanol column with methanol column
Tower bottoms is exported and methanol column boils kettle liquid entrance and is connected again；And ethanol propanol tower tower bottom reboiler, with ethanol propanol tower
Ethanol propanol tower bottoms is exported and ethanol propanol tower boils kettle liquid entrance and is connected again.
Further, three-tower differential pressure coupling rectification system, in addition to：Dehydrating tower tower reactor discharging cooler, with dehydrating tower
The outlet of dehydrating tower tower bottoms is connected.
Further, three-tower differential pressure coupling rectification system, in addition to：Methanol column overhead condenser, the methanol with methanol column
Column overhead steam condensate outlet and methanol tower top steam inlet are connected.
The three-tower differential pressure coupling rectification system separated using low carbon mixed alcohol of the present utility model, is steamed using dehydration column overhead
The pyrogen that vapour boils again with ethanol normal propyl alcohol column overhead steam as methanol column tower bottoms, is greatly reduced production cost and energy consumption, manages
By upper Finestill energy-saving nearly 30%.
Brief description of the drawings
The Figure of description for constituting the part of the application is used for providing further understanding to of the present utility model, this practicality
New schematic description and description is used to explain the utility model, does not constitute to improper restriction of the present utility model.
In the accompanying drawings：
Fig. 1 shows the structure and process flow diagram of the three-tower differential pressure coupling rectification system of embodiment 1；And
Fig. 2 shows the structure and process flow diagram of the traditional piece-rate system of the low carbon mixed alcohol of comparative example 1.
Embodiment
It should be noted that in the case where not conflicting, the feature in embodiment and embodiment in the application can phase
Mutually combination.Describe the utility model in detail below with reference to the accompanying drawings and in conjunction with the embodiments.
According to a kind of typical embodiment of the utility model, there is provided the three-tower differential pressure coupling that a kind of low carbon mixed alcohol is separated
Distillation system.As shown in figure 1, the three-tower differential pressure coupling rectification system include the dehydrating tower T-1, the methanol column T-2 that are sequentially communicated and
Ethanol propanol tower T-3, further comprises：Dehydrating tower primary condenser E-1, is provided with dehydration column overhead steam inlet, dehydrating tower
Overhead vapours is exported and methanol column tower bottoms first entrance, the outlet of the first gas phase mixture and the outlet of the first liquid phase mixture,
Dehydration column overhead steam (vapor) outlet on ethanol propanol tower T-3 path with being provided with ethanol propanol tower after-condenser E-8, the first gas
Phase mixture outlet is connected with methanol column T-2 tower reactor, and the outlet of the first liquid phase mixture is connected with ethanol propanol tower T-3；
And ethanol propanol tower primary condenser E-6, be provided with ethanol propanol overhead vapours entrance, ethanol propanol overhead vapours outlet with
And the outlet of methanol column tower bottoms second entrance, the second gas phase mixture and second liquid phase mixture outlet, the steaming of ethanol propanol tower top
Vapor outlet is with being provided with ethanol propanol tower after-condenser E-8, the outlet of the second gas phase mixture on ethanol propanol tower T-3 path
It is connected with methanol column T-2 tower reactor, second liquid phase mixture outlet is connected with ethanol propanol tower T-3.
The three-tower differential pressure coupling rectification system separated using low carbon mixed alcohol of the present utility model, dehydrating tower primary condenser
E-1 and ethanol propanol tower primary condenser E-6 are the reboilers as methanol column T-2, utilize dehydration column overhead steam and ethanol
The thermal source that normal propyl alcohol column overhead steam boils again as methanol column tower bottoms, had both saved dehydrating tower T-1 and ethanol propanol tower T-3 tower tops
The cooling load of condenser, saves the heating load of methanol column T-2 tower reactor reboilers, production cost and energy consumption is greatly reduced again,
Finestill energy-saving nearly 30% in theory.
According to a kind of typical embodiment of the utility model, in addition to：Dehydrating tower tower bottom reboiler E-3, with dehydrating tower
T-1 dehydrating tower tower bottoms outlet and dehydrating tower boil kettle liquid entrance and are connected again, methanol column bottom of towe auxiliary reboiler E-7, with first
Alcohol tower T-2 methanol column tower bottoms outlet and methanol column boil kettle liquid entrance and are connected again；And ethanol propanol tower tower bottom reboiler
E-9, the outlet of ethanol propanol tower bottoms and ethanol propanol tower with ethanol propanol tower T-3 are boiled kettle liquid entrance and are connected again.Methanol column
Under T-2 tower reactors thermic load and dehydrating tower T-1 and ethanol propanol tower T-3 tower top thermic load match condition, dehydrating tower time condensation
Device E-2, ethanol propanol tower after-condenser E-8 and methanol column auxiliary reboiler E-7 can be without opening.
It is preferred that, the three-tower differential pressure coupling rectification system also includes：Dehydrating tower tower reactor discharging cooler E-4, with dehydrating tower
T-1 dehydrating tower tower bottoms outlet is connected.It is preferred that, the three-tower differential pressure coupling rectification system also includes：Methanol column overhead is cold
Condenser E-5, the outlet of methanol column overhead vapours and methanol tower top steam inlet with methanol column T-2 are connected.
Using system of the present utility model, including using dehydrating tower T-1, methanol column T-2 and the ethanol propanol being sequentially communicated
Tower T-3 carries out rectifying, is boiled again as methanol column tower bottoms by the use of dehydration column overhead steam and ethanol normal propyl alcohol column overhead steam
Thermal source.
It is preferred that, when methanol column T-2 tower reactor thermic load and dehydrating tower T-1 and ethanol propanol tower T-3 tower top thermic load
Matching, without opening other heat-exchanger rigs.
It is preferred that, dehydrating tower T-1 operating pressure scope is 0.1-0.4MPa, and methanol column T-2 operating pressure scope is
0-0.1MPa, ethanol propanol tower T-3 operating pressure scope are 0.1-0.3MPa.
The beneficial effects of the utility model are further illustrated below in conjunction with embodiment.
Embodiment 1
The three-tower differential pressure coupling rectification system of low carbon mixed alcohol separation, including dehydrating tower T-1, methanol column T-2, ethanol propanol
Tower T-3, dehydrating tower primary condenser E-1, dehydrating tower after-condenser E-2, dehydrating tower tower bottom reboiler E-3, dehydrating tower tower reactor
Discharged cooler E-4, methanol column overhead condenser E-5, ethanol propanol tower primary condenser E-6, and methanol column bottom of towe auxiliary is boiled again
Device E-7, ethanol propanol tower after-condenser E-8, ethanol propanol tower tower bottom reboiler E-9.
Three-tower differential pressure coupling rectification technique：
As shown in figure 1, after mixed alcohol water 1 is separated through dehydrating tower T-1, dehydrating tower tower bottoms is divided into two parts, a part is de-
Water tower tower bottoms 5 is formed after being heated through dehydrating tower tower bottom reboiler E-3 boils vapour return dehydrating tower T-1, another part dehydrating tower again
Tower bottoms 6 discharges to discharge as waste water after cooler E-4 is cooled down through dehydrating tower tower reactor carries out lower step processing, dehydration column overhead steam
2 through dehydrating tower primary condenser E-1, after dehydrating tower after-condenser E-2 heat exchange condensations, by certain first-class stock 3 of reflux ratio
Backflow, second stock 4 enters methanol column T-2, and methanol column overhead vapours 7 is returned after methanol column overhead condenser E-5 by certain
Stream is flowed back than the 3rd stream stock 8, and the 4th stream stock 9 is produced as methanol product, and methanol column tower reactor liquid is divided into the 5th stream after pump P-1
The stream stock 13 of stock 10 and the 6th, after the 5th stream stock 10 exchanges heat through dehydrating tower primary condenser E-1, gas phase mixture 11 enters methanol column
T-2 tower reactors, the first liquid phase mixture 12 enters ethanol propanol tower T-3, and the 6th stream stock 13 can be divided into the 7th stream stream of stock 14 and the 8th
Stock 15, the 7th stream stock 14 is formed after aiding in reboiler E-7 heating through methanol column bottom of towe to boil vapour 17 and returns to methanol column T-2 again, the
After eight stream stocks 15 exchange heat through ethanol propanol tower primary condenser E-6, gas phase mixture 16 enters methanol column T-2 tower reactors, the second liquid
Phase mixture 18 enters ethanol propanol tower T-3, and ethanol propanol column overhead steam 20 is through ethanol propanol tower primary condenser E-6 and second
After alcohol propyl alcohol tower after-condenser E-8, flowed back by certain stream stock 21 of reflux ratio the 9th, the tenth stream stock 22 is produced, ethanol propanol
Tower tower bottoms is divided into two parts, shape after a part of ethanol propanol tower tower bottoms 23 is heated through ethanol propanol tower tower bottom reboiler E-9
Ethanol propanol tower T-3 is returned into vapour is boiled again, the extraction of another part ethanol propanol tower tower bottoms 24 is further processed.Wherein,
First liquid phase mixture 12 and the blended device V-1 of second liquid phase mixture 18 converge after the three one-tenth liquid phase mixtures 19 by pump P-
2 enter ethanol propanol tower T-3.
Mixed alcohol water inlet amount is 1942.403kg/h, and wherein the mass fraction of methanol is 20.7%, dehydrating tower T-1 operations
Pressure is 0.316MPa, and tower top temperature is 99.9 DEG C, and methanol column T-2 operating pressures are 0.050MPa, and tower top temperature is 48.0 DEG C,
Bottom temperature is 67.4 DEG C, and ethanol propanol tower T-3 operating pressures are 0.203MPa, and tower top temperature is 97.0 DEG C；Whole low-carbon alcohols
The total low-pressure steam consumption of hybrid separation system is about 4.98 ton/ton products.
Comparative example 1
Low carbon mixed alcohol tradition separating technology：
As shown in Fig. 2 traditional separating technology system includes dehydrating tower T-1, methanol column T-2, ethanol propanol tower T-3, dehydration
Column overhead condenser E-1, dehydrating tower tower bottom reboiler E-3, dehydrating tower tower reactor discharging cooler E-4, methanol column overhead condenser
E-5, methanol column tower bottom reboiler E-7, ethanol propanol column overhead condenser E-6, ethanol propanol tower tower bottom reboiler E-9.
After mixed alcohol water 1 is separated through dehydrating tower T-1, dehydrating tower tower bottoms is divided into two parts, a part of dehydrating tower tower bottoms 5
Formed after being heated through dehydrating tower tower bottom reboiler E-3 and boil vapour return dehydrating tower T-1 again, another part dehydrating tower tower bottoms 6 is through de-
Lower step processing is carried out as waste water discharge after the discharging cooler E-4 coolings of water tower tower reactor, dehydration column overhead steam 2 is through dehydrating tower tower
Push up after condenser E-1 heat exchange condensations, flowed back by certain first-class stock 3 of reflux ratio, second stock 4 enters methanol column T-2, methanol
Tower T-2 overhead vapours 7 flows back after methanol column overhead condenser E-5 heat exchange condensations by certain stream stock 8 of reflux ratio the 3rd, the
Four stream stocks 9 are produced as methanol product, and methanol column tower bottoms is divided into two parts, and a part of methanol column tower bottoms 10 is through methanol column tower
Formed after bottom reboiler E-7 heating and boil vapour return methanol column T-2 again, another part methanol column tower bottoms 11 enters ethanol propanol tower
T-3, ethanol propanol column overhead steam 12 flows back after ethanol propanol tower condenser E-6 by certain stream stock 13 of reflux ratio the 5th,
6th stream stock 14 is produced, and ethanol propanol tower tower bottoms is divided into two parts, and a part of ethanol propanol tower tower bottoms 15 is through ethanol propanol
Formed after tower tower bottom reboiler E-9 heating and boil vapour return ethanol propanol tower T-3 again, another part ethanol propanol tower tower bottoms 16 is adopted
Go out to be further processed.
Using traditional separating technology, whole low-carbon alcohols hybrid separation system consumes about 7.2 tons of low-pressure steam/ton products altogether,
And use after three-tower differential pressure coupling process, the total low-pressure steam consumption of whole low-carbon alcohols hybrid separation system is about 4.98 tons/
Ton product, energy-conservation nearly 30%.
As can be seen from the above description, the utility model the above embodiments realize following technique effect：
The three-tower differential pressure coupling rectification system separated using low carbon mixed alcohol of the present utility model, utilizes dehydration column overhead work
The condensation latent heat of skill gas and ethanol normal propyl alcohol column overhead process gas, instead of methanol column tower reactor low-pressure steam in traditional handicraft,
Production cost and energy consumption is greatly reduced, in theory Finestill energy-saving nearly 30%.
Preferred embodiment of the present utility model is the foregoing is only, the utility model is not limited to, for this
For the technical staff in field, the utility model can have various modifications and variations.It is all it is of the present utility model spirit and principle
Within, any modification, equivalent substitution and improvements made etc. should be included within protection domain of the present utility model.
Claims (4)
1. a kind of three-tower differential pressure coupling rectification system of low carbon mixed alcohol separation, including dehydrating tower (T-1), the methanol being sequentially communicated
Tower (T-2) and ethanol propanol tower (T-3), it is characterised in that further comprise：
Dehydrating tower primary condenser (E-1), is provided with dehydration column overhead steam inlet, dehydration column overhead steam (vapor) outlet and methanol
Tower tower bottoms first entrance, the outlet of the first gas phase mixture and the outlet of the first liquid phase mixture, the dehydration column overhead steam go out
Mouth is with being provided with dehydrating tower after-condenser (E-2), the first gas phase mixture outlet on the path of the dehydrating tower (T-1)
It is connected with the tower reactor of the methanol column (T-2), the first liquid phase mixture outlet is connected with the ethanol propanol tower (T-3)
It is logical；And
Ethanol propanol tower primary condenser (E-6), is provided with ethanol propanol overhead vapours entrance, the outlet of ethanol propanol overhead vapours
And the outlet of methanol column tower bottoms second entrance, the second gas phase mixture and second liquid phase mixture outlet, the ethanol propanol
Overhead vapours exports and is provided with ethanol propanol tower after-condenser (E-8) on the path with the ethanol propanol tower (T-3), described
Second gas phase mixture outlet is connected with the tower reactor of the methanol column (T-2), the second liquid phase mixture outlet with it is described
Ethanol propanol tower (T-3) is connected.
2. three-tower differential pressure coupling rectification system according to claim 1, it is characterised in that also include：
Kettle liquid is boiled in dehydrating tower tower bottom reboiler (E-3), the outlet of dehydrating tower tower bottoms and dehydrating tower with the dehydrating tower (T-1) again
Entrance is connected,
Methanol column bottom of towe auxiliary reboiler (E-7), the outlet of methanol column tower bottoms and methanol column with the methanol column (T-2) are boiled again
Kettle liquid entrance is connected；And
Ethanol propanol tower tower bottom reboiler (E-9), the outlet of ethanol propanol tower bottoms and ethanol with the ethanol propanol tower (T-3)
Propyl alcohol tower boils kettle liquid entrance and is connected again.
3. three-tower differential pressure coupling rectification system according to claim 1, it is characterised in that also include：Dehydrating tower tower reactor goes out
Expect cooler (E-4), be connected with the dehydrating tower tower bottoms outlet of the dehydrating tower (T-1).
4. three-tower differential pressure coupling rectification system according to claim 1, it is characterised in that also include：Methanol column overhead is cold
Condenser (E-5), is connected with the methanol column overhead vapours condensate outlet of the methanol column (T-2) and methanol tower top steam inlet
It is logical.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720104741.3U CN206494868U (en) | 2017-01-23 | 2017-01-23 | A kind of three-tower differential pressure coupling rectification system of low carbon mixed alcohol separation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720104741.3U CN206494868U (en) | 2017-01-23 | 2017-01-23 | A kind of three-tower differential pressure coupling rectification system of low carbon mixed alcohol separation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206494868U true CN206494868U (en) | 2017-09-15 |
Family
ID=59804185
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201720104741.3U Active CN206494868U (en) | 2017-01-23 | 2017-01-23 | A kind of three-tower differential pressure coupling rectification system of low carbon mixed alcohol separation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206494868U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107915580A (en) * | 2017-10-27 | 2018-04-17 | 烟台国邦化工机械科技有限公司 | A kind of ethylene glycol multi-effect distillation system and process |
-
2017
- 2017-01-23 CN CN201720104741.3U patent/CN206494868U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107915580A (en) * | 2017-10-27 | 2018-04-17 | 烟台国邦化工机械科技有限公司 | A kind of ethylene glycol multi-effect distillation system and process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100584421C (en) | Differential pressure low-energy-consumption distillation method and equipment | |
| CN100378051C (en) | Rectifying tech. and equipment of high purity methanol | |
| CN107812393A (en) | A kind of methanol three-effect rectification system and technique | |
| CN108101748B (en) | Four-tower three-effect methanol rectification energy-saving process method and device | |
| CN106478368B (en) | Produce the energy-saving rectifying process and device of high grade edible spirit | |
| CN111437619B (en) | Multi-tower differential pressure energy-saving absolute alcohol distillation system and absolute alcohol energy-saving production method | |
| CN101195561B (en) | Method for producing dimethyl ether with methanol gas-phase dehydration | |
| CN111116317A (en) | Five-tower four-effect methanol rectification process and equipment | |
| CN102875329B (en) | A kind of heat pump distillation is separated technique and the device of primary isoamyl alcohol isomers | |
| CN110256202A (en) | A kind of refining crude methanol process of four towers quadruple effect | |
| CN106588572A (en) | Three-tower differential pressure coupling rectifying system and method separating low-carbon mixed alcohols | |
| CN106745421A (en) | A kind of multiple Intermediate Heat Exchanger rectification method treatment low concentration DMF waste water systems of band | |
| CN107754365A (en) | A kind of double effect rectification for methanol refining plant and process | |
| CN206494868U (en) | A kind of three-tower differential pressure coupling rectification system of low carbon mixed alcohol separation | |
| CN109646980A (en) | Without the tower-coupled methanol multi-effect distillation energy saver in fusel oil next door and method | |
| CN107551586A (en) | A kind of device using next door tower combination multi-effect distillation production methanol | |
| CN208883743U (en) | A kind of refining crude methanol process system of three towers triple effect | |
| CN105964007A (en) | Equipment and process for separating n-butyl alcohol-isobutyl alcohol mixture | |
| CN213760551U (en) | 1-butene refining energy-saving device with heat pump heat integration | |
| CN104606910A (en) | Heat pump rectifying device based on heat storage technology and starting method of heat pump rectifying device | |
| CN213760550U (en) | Two-tower double-heat-pump integrated 1-butene refining energy-saving device | |
| CN207532818U (en) | A kind of methanol three-effect rectification system | |
| CN208292896U (en) | The methanol recovery device of methyl tertiary butyl ether(MTBE) production | |
| CN210314061U (en) | Rectification and purification device for synthesizing dimethyl oxalate by carbonylation of coal-made ethylene glycol | |
| CN208995418U (en) | A kind of acetic synthesis separation and recovery of catalyst device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |