CN208500801U - A kind of ethyl alcohol process units - Google Patents
A kind of ethyl alcohol process units Download PDFInfo
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- CN208500801U CN208500801U CN201721778147.9U CN201721778147U CN208500801U CN 208500801 U CN208500801 U CN 208500801U CN 201721778147 U CN201721778147 U CN 201721778147U CN 208500801 U CN208500801 U CN 208500801U
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- rectifying column
- ethyl alcohol
- steam
- tower
- rectifying
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Utility model is related to a kind of ethyl alcohol process units.It include: rectifying column, for carrying out rectifying separation to the reaction mass produced by synthesis gas containing ethyl alcohol；Overhead condenser is connected to the side line or tower top of rectifying column, for carrying out the tower top that partial condensation is back to rectifying column to the steam of extraction；The permeable film device of Steam soak is connected to the steam discharge port of overhead condenser, for being dehydrated to steam material；It is connected between the permeable film device of Steam soak and overhead condenser by superheater and/or heat pump；Heat exchange connection is carried out by First Heat Exchanger between the outlet of material side and the material inlet of rectifying column of the permeable film device of Steam soak；The materials at bottom of tower of rectifying column, which is exported, carries out heat exchange connection by the second heat exchanger between the material inlet of rectifying column；The tower bottom of rectifying column also sets up reboiler.
Description
Technical field
The utility model relates to a kind of ethyl alcohol process units, in particular to a kind of synthesis gas prepare ethyl alcohol dewatering process and
Device.
Background technique
Ethyl alcohol all has been widely used in national defence chemical industry, health care, food industry, industrial and agricultural production.Ethyl alcohol production
Method has biological fermentation process and chemical synthesis.Wherein to prepare ethyl alcohol production technology mature for synthesis gas in chemical synthesis, raw
It produces cost and is substantially less than grain route, there is stronger competitiveness and broad based growth prospect.Synthesis gas produces there are three types of ethyl alcohol, and one
It is synthesis gas ethyl alcohol directly processed；Second is that synthesis gas biology legal system ethyl alcohol；Third is that synthesis gas is through acetic acid preparation of ethanol by hydrogenating.No matter which kind of
Method ethanol production obtains aqueous ethyl alcohol.Since second alcohol and water is there are azeotropic point, conventional method can not directly obtain anhydrous
Ethyl alcohol.The methods of sequence of constant boiling and rectification, extracting rectifying and adsorbing separation are mainly taken in the production of industry anhydrous ethanol at present, these tradition
Ethanol dehydration mode all there is the problems such as process is complicated, energy consumption is high and seriously polluted.
Film dehydration technique is different from diffusion rate using (absorption) is dissolved in film by each component in separation of liquid mixtures
And realize separation, be a kind of new separation technology, have it is energy-efficient, process is easily controllable, it is easy to operate, convenient for amplification and produce
The advantages of industry.Its advantage protruded is that separation process is not limited by component vapor liquid equilibrium, can realize rectifying with low energy consumption
Etc. conventional methods be difficult to completing for task, such as the separation of azeotropic, nearly boiling mixture.
Utility model content
The purpose of the utility model is to provide the dewatering process that a kind of synthesis gas prepares ethyl alcohol, using rectifying-Steam soak
Traditional handicraft is coupled with new separation technology, is not limited by azeotropic by permeable film device coupling technique, is not required to addition third group
Point, it is a kind of isolation technics of high-efficient energy-saving environment friendly.
A kind of method ethanol production, includes the following steps:
Step 1 produces the reaction mass containing ethyl alcohol by synthesis gas；
Got in step 1 reaction mass is carried out rectifying separation, tower top or side in the last one rectifying column by step 2
Line produces the steam containing ethyl alcohol；
Step 3, the steam containing ethyl alcohol that step 2 is obtained, which is sent into vapor permeable membrane, to be dehydrated, and obtains ethyl alcohol production
Product.
In one embodiment, in the step 2, aqueous 0.1~30wt% in the steam containing ethyl alcohol.
In one embodiment, in the step 3, aqueous 0.01~1wt% in alcohol product.
In one embodiment, in the step 3, the operating pressure of the feed liquid side of vapor permeable membrane is 100~600
KPa, operation temperature are 10~20 DEG C of the corresponding temperature overheating of saturated vapor pressure of charging.
In one embodiment, in the step 3, vapor permeable membrane selected from molecular screen membrane, silicon dioxide film or
PVA film, preferred molecular sieve film.
In one embodiment, the step 1 produces the reaction mass containing ethyl alcohol by synthesis gas and is selected from conjunction
At gas ethyl alcohol directly processed, synthesis gas biology legal system ethyl alcohol, synthesis gas through acetic acid preparation of ethanol by hydrogenating, synthesis gas through acetic acid ester through hydrogenation system
One of ethyl alcohol.
A kind of ethyl alcohol process units, comprising:
Rectifying column, for carrying out rectifying separation to the reaction mass produced by synthesis gas containing ethyl alcohol；
Overhead condenser is connected to the side line or tower top of rectifying column, returns for carrying out partial condensation to the steam of extraction
It flow to the tower top of rectifying column；
The permeable film device of Steam soak is connected to the steam discharge port of overhead condenser, for taking off to steam material
Water；
It is connected between the permeable film device of Steam soak and overhead condenser by superheater and/or heat pump；
Pass through First Heat Exchanger between the outlet of material side and the material inlet of rectifying column of the permeable film device of Steam soak
Carry out heat exchange connection；
The materials at bottom of tower of rectifying column, which is exported, carries out heat exchange connection by the second heat exchanger between the material inlet of rectifying column；
The tower bottom of rectifying column also sets up reboiler.
Vapor permeable membrane in the permeable film device of the Steam soak is selected from molecular screen membrane, silicon dioxide film or PVA
Film, preferred molecular sieve film.
It further include Salt Addition Extraction Refinery Tower, the tower top outlet of Salt Addition Extraction Refinery Tower is connected to the material inlet of rectifying column,
For removing the methyl acetate in raw material.
Beneficial effect
1, the utility model is dehydrated using the permeable film device coupling technique of rectifying-Steam soak, is not limited by azeotropic,
It is not required to addition third component, is a kind of isolation technics of high-efficiency environment friendly.2, the utility model the top of the distillation column or side line gas phase are straight
It taps into film device, compared with traditional handicraft, 20% or more energy conservation.
Detailed description of the invention
Fig. 1 is the flow diagram for the dewatering process that synthesis gas used in Example 1 prepares ethyl alcohol.
Fig. 2 is the flow diagram for the dewatering process that the synthesis gas used in embodiment 2 prepares ethyl alcohol；Fig. 3 is embodiment 4
The synthesis gas of use prepares the flow diagram of the dewatering process of ethyl alcohol.
Wherein, 1, First Heat Exchanger；2, First Heat Exchanger；3, rectifying column；4, reboiler；5, overhead condenser；6, it overheats
Device；7, the permeable film device of Steam soak；8, heat pump；9, Salt Addition Extraction Refinery Tower.
Specific embodiment
Embodiment 1
As shown in Figure 1, (containing 65wt%H with synthesis gas2, 30wt%CO) the direct synthesizing alcohol under Cu-Co catalyst system,
Reaction product after fixed gas separates, obtain containing 62wt% ethyl alcohol, 20wt% methanol, 13wt% water steam, be sent into rectifying column
Middle carry out rectifying, rectifying tower pressure interior force 300kPa, 86 DEG C of column bottom temperature, 74 DEG C of tower top temperature, from overhead extraction methanol, from side line
It produces ethyl alcohol (aqueous 8wt%), by the material of side take-off after heat exchange, overheat, is sent into vapor permeable membrane and is taken off
Water, vapor permeable membrane is using NaA molecular sieve membrane, 114 DEG C of feed liquid side temperature, feed liquid side absolute pressure 120kPa, per-meate side absolute pressure
1000Pa, vapor permeable membrane average water flux 0.98kg/m2H, per-meate side obtain the alcohol product of aqueous 0.5wt%.
Embodiment 2
As shown in Fig. 2, (containing 65wt%H with synthesis gas2, 30wt%CO) in CO as carbon source, using fermentation legal system ethyl alcohol
(CN105755058A), fermentation liquid is sent into rectifying column after filtering out thallus and carries out rectifying, rectifying tower pressure interior force 300kPa,
88 DEG C of column bottom temperature, 78 DEG C of tower top temperature, from overhead extraction ethyl alcohol (aqueous 16wt%), by the material of side take-off through heat exchange,
After overheat, it is sent into vapor permeable membrane and is dehydrated, vapor permeable membrane is using NaA molecular sieve membrane, feed liquid side temperature 110
DEG C, feed liquid side absolute pressure 150kPa, per-meate side absolute pressure 1500Pa, vapor permeable membrane average water flux 0.98kg/m2H, per-meate side
Obtain the alcohol product of aqueous 0.8wt%.
Embodiment 3
As shown in Fig. 2, (containing 65wt%H with synthesis gas2, 30wt%CO) reaction generate dimethyl ether (CH3OCH3), dimethyl ether carbonyl
For base metaplasia at methyl acetate, methyl acetate adds hydrogen that methanol and ethyl alcohol (CN104710282A) is made under the effect of the catalyst, contains
Rectifying, rectifying tower pressure interior force are carried out in the product feeding rectifying column for having 54wt% methanol, 34wt% ethyl alcohol, 9wt% methyl acetate
350kPa, 88 DEG C of column bottom temperature, 76 DEG C of tower top temperature, will from side take-off ethyl alcohol (aqueous 1.2wt%) from overhead extraction methanol
The material of side take-off after heat exchange, overheat, be sent into vapor permeable membrane in be dehydrated, vapor permeable membrane using
NaA molecular sieve membrane, 105 DEG C of feed liquid side temperature, feed liquid side absolute pressure 80kPa, per-meate side absolute pressure 500Pa, vapor permeable membrane average water
Flux 0.93kg/m2H, per-meate side obtain the alcohol product of aqueous 0.08wt%.
Embodiment 4
As shown in figure 3, (containing 65wt%H with synthesis gas2, 30wt%CO) reaction generate dimethyl ether (CH3OCH3), dimethyl ether carbonyl
For base metaplasia at methyl acetate, methyl acetate adds hydrogen that methanol and ethyl alcohol (CN104710282A) is made under the effect of the catalyst, contains
There is the product of 54wt% methanol, 34wt% ethyl alcohol, 9wt% methyl acetate using extractive distillation with salt method separating acetic acid methyl esters, it will be upper
The reaction product stated is sent into Salt Addition Extraction Refinery Tower 9, and 9 tower top of Salt Addition Extraction Refinery Tower is equipped with refluxing opening, the extractant of reflux
It is 1:1, Salt Addition Extraction Refinery Tower for the water reaction product of the potassium acetate containing 0.1g/ml and the charge-mass ratio of extractant adopted
Interior is normal pressure, and 87 DEG C of column bottom temperature, 73 DEG C of tower top temperature, overhead vapours produces import of the mouth after condenser with rectifying column 3
Connection, from obtained in 9 overhead vapours of Salt Addition Extraction Refinery Tower methanol containing 55wt%, 32wt% ethyl alcohol, 11wt% water except the alcohol after ester
Class product, then alcohol product is sent into rectifying column 3 and carries out rectifying, rectifying tower pressure interior force 350kPa, 88 DEG C of column bottom temperature, tower top
76 DEG C of temperature, from overhead extraction methanol, from side take-off ethyl alcohol (aqueous 1.6wt%), by the material of side take-off through heat exchange,
After overheat, it is sent into vapor permeable membrane and is dehydrated, vapor permeable membrane is using NaA molecular sieve membrane, feed liquid side temperature 105
DEG C, feed liquid side absolute pressure 80kPa, per-meate side absolute pressure 500Pa, vapor permeable membrane average water flux 1.06kg/m2H, per-meate side obtain
To the alcohol product of aqueous 0.08wt%.In the present embodiment, the acetic acid in methanol and ethyl alcohol is isolated using extractive distillation with salt
Methyl esters, and the extractant being entrained with is placed in the distillation process of methanol, ethyl alcohol and synchronizes separation, it realizes same by rectifying
When removal product in the extractant carried secretly, while realizing the separation of the methanol and ethyl alcohol in distillation process again, then pass through steam
Permeable membrane is dehydrated hydrous ethanol, also improves the water flux of Steam soak process.
Claims (3)
1. a kind of ethyl alcohol process units characterized by comprising
Rectifying column (3), for carrying out rectifying separation to the reaction mass produced by synthesis gas containing ethyl alcohol；
Overhead condenser (5) is connected to the side line or tower top of rectifying column (3), for carrying out partial condensation to the steam of extraction
It is back to the tower top of rectifying column (3)；
The permeable film device of Steam soak (7) is connected to the steam discharge port of overhead condenser (5), for carrying out to steam material
Dehydration；
It is connected between the permeable film device of Steam soak (7) and overhead condenser (5) by superheater (6) and/or heat pump (8)；
Pass through the first heat exchange between the outlet of the material side of the permeable film device of Steam soak (7) and the material inlet of rectifying column (3)
Device (1) carries out heat exchange connection；
The materials at bottom of tower of rectifying column (3), which is exported, to be exchanged heat between the material inlet of rectifying column (3) by the second heat exchanger (2)
Connection；
The tower bottom of rectifying column (3) also sets up reboiler (4).
2. ethyl alcohol process units according to claim 1, which is characterized in that the permeable film device of the Steam soak (7)
In vapor permeable membrane be selected from molecular screen membrane, silicon dioxide film or PVA film.
3. ethyl alcohol process units according to claim 1, which is characterized in that further include Salt Addition Extraction Refinery Tower (9), add salt
The tower top outlet of extractive distillation column (9) is connected to the material inlet of rectifying column (3), for removing the methyl acetate in raw material.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721778147.9U CN208500801U (en) | 2017-12-19 | 2017-12-19 | A kind of ethyl alcohol process units |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721778147.9U CN208500801U (en) | 2017-12-19 | 2017-12-19 | A kind of ethyl alcohol process units |
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| Publication Number | Publication Date |
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| CN208500801U true CN208500801U (en) | 2019-02-15 |
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| CN201721778147.9U Active CN208500801U (en) | 2017-12-19 | 2017-12-19 | A kind of ethyl alcohol process units |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116003233A (en) * | 2022-12-16 | 2023-04-25 | 南京长江江宇环保科技股份有限公司 | Method for separating mixture of water, acetone and methyl acetate |
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2017
- 2017-12-19 CN CN201721778147.9U patent/CN208500801U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116003233A (en) * | 2022-12-16 | 2023-04-25 | 南京长江江宇环保科技股份有限公司 | Method for separating mixture of water, acetone and methyl acetate |
| CN116003233B (en) * | 2022-12-16 | 2024-01-05 | 南京长江江宇环保科技股份有限公司 | Method for separating mixture of water, acetone and methyl acetate |
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