CN203874490U - Ethanol distillation system - Google Patents
Ethanol distillation system Download PDFInfo
- Publication number
- CN203874490U CN203874490U CN201420227877.XU CN201420227877U CN203874490U CN 203874490 U CN203874490 U CN 203874490U CN 201420227877 U CN201420227877 U CN 201420227877U CN 203874490 U CN203874490 U CN 203874490U
- Authority
- CN
- China
- Prior art keywords
- tower
- ethanol recovery
- pressure ethanol
- recovery tower
- methyl alcohol
- 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.)
- Expired - Lifetime
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 203
- 238000004821 distillation Methods 0.000 title claims abstract description 12
- OKKJLVBELUTLKV-UHFFFAOYSA-N methanol Natural products OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 126
- 238000011084 recovery Methods 0.000 claims abstract description 66
- -1 methanol ester Chemical class 0.000 claims abstract description 31
- 239000007792 gaseous phase Substances 0.000 claims description 8
- 239000003513 alkali Substances 0.000 claims description 5
- 230000018044 dehydration Effects 0.000 claims description 5
- 238000006297 dehydration reaction Methods 0.000 claims description 5
- 239000002808 molecular sieve Substances 0.000 claims description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 5
- 238000000926 separation method Methods 0.000 abstract description 9
- 238000000034 method Methods 0.000 abstract description 8
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 239000006227 byproduct Substances 0.000 abstract 1
- 230000008520 organization Effects 0.000 abstract 1
- 239000000047 product Substances 0.000 abstract 1
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 28
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 10
- 239000000203 mixture Substances 0.000 description 10
- XBDQKXXYIPTUBI-UHFFFAOYSA-M Propionate Chemical compound CCC([O-])=O XBDQKXXYIPTUBI-UHFFFAOYSA-M 0.000 description 9
- KXKVLQRXCPHEJC-UHFFFAOYSA-N acetic acid trimethyl ester Natural products COC(C)=O KXKVLQRXCPHEJC-UHFFFAOYSA-N 0.000 description 9
- 239000007789 gas Substances 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 238000009833 condensation Methods 0.000 description 5
- 230000005494 condensation Effects 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 150000002148 esters Chemical class 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000010533 azeotropic distillation Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000010189 synthetic method Methods 0.000 description 1
Abstract
The utility model discloses an ethanol distillation system which comprises a light component removal tower, a high-pressure ethanol recovery tower, a low-pressure ethanol recovery tower and a methanol ester separation tower. According to the system, based on a four-tower process, crude ethanol sequentially passes through the light component removal tower, the high-pressure ethanol recovery tower, the low-pressure ethanol recovery tower and the methanol ester separation tower; the characteristics of an ethanol production process are fully utilized, the organization of the technical process and the setting of the separation target are reasonable, operation parameters of each distillation tower are optimized, a combined high/low-pressure distillation process is adopted, the characteristic that an azeotrope is easily formed among a part of components is utilized, partial byproducts are subjected to fuzzy separation, and finally the products ethanol and methanol are obtained.
Description
Technical field
The utility model belongs to chemical technology field, particularly a kind of from the mixture containing ethanol, methyl alcohol, ethyl acetate and/or methyl acetate the distillation system of separating alcohol and methanol product.
Background technology
In synthetic method, produce in ethanol, in coarse ethanol, contain accessory substance and the impurity such as hydrogen, alkane, dimethyl ether, methyl alcohol, ethyl acetate, methyl acetate, in order to obtain qualified alcohol product and to reclaim accessory substance, need to carry out rectifying separation to coarse ethanol.
Due to the composition more complicated of coarse ethanol, the relative volatility between each component is smaller, and easily forms azeotropic mixture between part component, these components is carried out to complete separation more difficult, needs to consume a large amount of energy, causes the production cost of product to increase.
Utility model content
Goal of the invention of the present utility model is: for the problem of above-mentioned existence, provide a kind of energy-saving ethanol distillation system.
The technical solution of the utility model is achieved in that ethanol distillation system, it is characterized in that: comprise lights removal tower, high-pressure ethanol recovery tower, low pressure ethanol recovery tower and methyl alcohol ester knockout tower, the tower top of described lights removal tower is connected with segregator, the tower reactor of lights removal tower is connected with high-pressure ethanol recovery tower, the tower top of described high-pressure ethanol recovery tower is connected with methyl alcohol ester knockout tower, the tower reactor of high-pressure ethanol recovery tower is connected with low pressure ethanol recovery tower, the top gaseous phase of described high-pressure ethanol recovery tower is connected with low pressure ethanol recovery tower reboiler, the tower top of described low pressure ethanol recovery tower is connected with methyl alcohol ester knockout tower, the tower reactor of low pressure ethanol recovery tower is connected with molecular sieve dehydration system, treated output alcohol product, the top gaseous phase of described low pressure ethanol recovery tower is connected with low pressure ethanol recovery tower condenser with methyl alcohol ester knockout tower reboiler respectively, the tower top of described methyl alcohol ester knockout tower is connected with other operations, the tower reactor output methanol product of methyl alcohol ester knockout tower.
Ethanol distillation system described in the utility model, described in it, lights removal tower bottom adds pump to be connected with alkali lye.
The utility model adopts four-column process flow, make coarse ethanol successively by lights removal tower, high-pressure ethanol recovery tower, low pressure ethanol recovery tower, methyl alcohol ester knockout tower, make full use of the feature of alcohol production technique, reasonably organize technological process and definite separate targets, optimize each rectifying column operating parameter, and adopt high/low pressure rectifying group technology, utilize the feature that easily forms azeotropic mixture between part component, part accessory substance is carried out to fuzzy separation, finally obtain product ethanol and methyl alcohol.
Accompanying drawing explanation
Fig. 1 is process flow diagram of the present utility model.
Mark in figure: 1 is lights removal tower, 2 is high-pressure ethanol recovery tower, and 3 is low pressure ethanol recovery tower, and 4 is methyl alcohol ester knockout tower, and 5 is molecular sieve dehydration system, 6 add pump for alkali lye.
The specific embodiment
Below in conjunction with accompanying drawing, the utility model is described in detail.
In order to make the purpose of this utility model, technical scheme and advantage clearer, below in conjunction with drawings and Examples, the utility model is further elaborated.Should be appreciated that specific embodiment described herein is only in order to explain the utility model, and be not used in restriction the utility model.
As shown in Figure 1, ethanol distillation system, comprise lights removal tower 1, high-pressure ethanol recovery tower 2, low pressure ethanol recovery tower 3 and methyl alcohol ester knockout tower 4, the tower top of described lights removal tower 1 is connected with segregator, the tower reactor of lights removal tower 1 is connected with high-pressure ethanol recovery tower 2, described lights removal tower 1 bottom adds pump 6 to be connected with alkali lye, the tower top of described high-pressure ethanol recovery tower 2 is connected with methyl alcohol ester knockout tower 4, the tower reactor of high-pressure ethanol recovery tower 2 is connected with low pressure ethanol recovery tower 3, the top gaseous phase of described high-pressure ethanol recovery tower 2 is connected with low pressure ethanol recovery tower reboiler, the tower top of described low pressure ethanol recovery tower 3 is connected with methyl alcohol ester knockout tower 4, the tower reactor of low pressure ethanol recovery tower 3 is connected with molecular sieve dehydration system 5, treated output alcohol product, the top gaseous phase of described low pressure ethanol recovery tower 3 is connected with low pressure ethanol recovery tower condenser with methyl alcohol ester knockout tower reboiler respectively, the tower top of described methyl alcohol ester knockout tower 4 is connected with other operations, the tower reactor output methanol product of methyl alcohol ester knockout tower 4.
Ethanol rectification process flow process of the present utility model:
A), first coarse ethanol enters lights removal tower, remove the light component in coarse ethanol, as dimethyl ether and hydrogen, alkane etc., the tower top of lights removal tower adopts segregator, fixed gas is the light component such as hydrogen, methane and a small amount of dimethyl ether, fixed gas row torch, condensate liquid is the dimethyl ether containing a small amount of methyl alcohol, condensate liquid part is as overhead reflux, part extraction gives other operations as raw material, the tower reactor discharging of lights removal tower is the mixture of methyl alcohol, ethanol, ester and water, send high-pressure ethanol recovery tower; In the bottom of described lights removal tower, add a small amount of alkali lye, the acetic acid in neutralized crude ethanol.
B), in high-pressure ethanol recovery tower, methyl alcohol and ester are carried out to part separation, due to methyl acetate, ethyl acetate and the formation of methanol azeotropic mixture, what at the tower top of high-pressure ethanol recovery tower, obtain is methyl alcohol and most methyl acetate, ethyl acetate, the ethanol that only has minute quantity, the overhead product of high-pressure ethanol recovery tower send methyl alcohol ester knockout tower, the tower reactor of high-pressure ethanol recovery tower is methyl alcohol, ethanol, the mixture of ester and water, send low pressure ethanol recovery tower, simultaneously, the top gaseous phase of high-pressure ethanol recovery tower send low pressure ethanol recovery tower reboiler as thermal source, corresponding gas phase is condensed, at this, utilize methyl alcohol and methyl acetate, methyl alcohol and ethyl acetate to form the feature of low boiling azeotropic mixture, at high-pressure ethanol recovery tower, carry out azeotropic distillation, boiling point and the very approaching ethyl acetate of ethanol are separated from ethanol.
C), in low pressure ethanol recovery tower, methyl alcohol and ester in further separating alcohol, the overhead product of low pressure ethanol recovery tower is methyl alcohol and a small amount of methyl acetate, the ethanol of ethyl acetate and minute quantity, the overhead product of low pressure ethanol recovery tower send methyl alcohol ester knockout tower, the tower reactor product of low pressure ethanol recovery tower is ethanol and a small amount of water and micro-methyl alcohol, the tower reactor product of low pressure ethanol recovery tower is product ethanol after molecular sieve dehydration system removes part water, simultaneously, the top gaseous phase of low pressure ethanol recovery tower partly send methyl alcohol ester knockout tower reboiler as thermal source, corresponding gas phase is condensed, the condensation in the condenser being cooled with circulating water of another part gas phase.
D), in methyl alcohol ester knockout tower, because methyl alcohol and methyl acetate, ethyl acetate form azeotropic mixture, at the tower top of methyl alcohol ester knockout tower, obtain the azeotropic mixture of methyl acetate, ethyl acetate and methyl alcohol, give other operations as raw material, the tower reactor of methyl alcohol ester knockout tower is highly purified methanol product.
Wherein, because dimethyl ether, ethyl acetate, methyl acetate can give other operations as raw material, therefore for energy-conservation, these three kinds of accessory substances are only carried out to fuzzy separation; Optimize the operating parameter of rectifying columns at different levels, the operating pressure scope of described high-pressure ethanol recovery tower is 3～8barg, makes tower overhead gas condensation in low pressure ethanol recovery tower reboiler of high-pressure ethanol recovery tower; The operating pressure scope of described low pressure ethanol recovery tower is 0～2.5barg, make tower bottom reboiler by the tower overhead gas condensation heat supply of high-pressure ethanol recovery tower, tower overhead gas part condensation in methyl alcohol ester knockout tower reboiler of low pressure ethanol recovery tower, part condensation in water cooler, and tower reactor obtains alcohol product; The operating pressure scope of described methyl alcohol ester knockout tower is vacuum～1barg, makes the overhead gas of part low pressure ethanol recovery tower as methyl alcohol ester knockout tower reboiler heat source.By after optimizing, the rectifying column reboiler that rectifying column condenser that operating temperature is high and operating temperature are low is coupled, reach energy-conservation object.
The foregoing is only preferred embodiment of the present utility model; not in order to limit the utility model; all any modifications of doing within spirit of the present utility model and principle, be equal to and replace and improvement etc., within all should being included in protection domain of the present utility model.
Claims (2)
1. ethanol distillation system, it is characterized in that: comprise lights removal tower (1), high-pressure ethanol recovery tower (2), low pressure ethanol recovery tower (3) and methyl alcohol ester knockout tower (4), the tower top of described lights removal tower (1) is connected with segregator, the tower reactor of lights removal tower (1) is connected with high-pressure ethanol recovery tower (2), the tower top of described high-pressure ethanol recovery tower (2) is connected with methyl alcohol ester knockout tower (4), the tower reactor of high-pressure ethanol recovery tower (2) is connected with low pressure ethanol recovery tower (3), the top gaseous phase of described high-pressure ethanol recovery tower (2) is connected with low pressure ethanol recovery tower reboiler, the tower top of described low pressure ethanol recovery tower (3) is connected with methyl alcohol ester knockout tower (4), the tower reactor of low pressure ethanol recovery tower (3) can be connected with molecular sieve dehydration system (5), treated output alcohol product, the top gaseous phase of described low pressure ethanol recovery tower (3) is connected with low pressure ethanol recovery tower condenser with methyl alcohol ester knockout tower reboiler respectively, the tower top of described methyl alcohol ester knockout tower (4) is connected with other operations, the tower reactor output methanol product of methyl alcohol ester knockout tower (4).
2. ethanol distillation system according to claim 1, is characterized in that: described lights removal tower (1) bottom adds pump (6) to be connected with alkali lye.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420227877.XU CN203874490U (en) | 2014-05-06 | 2014-05-06 | Ethanol distillation system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420227877.XU CN203874490U (en) | 2014-05-06 | 2014-05-06 | Ethanol distillation system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203874490U true CN203874490U (en) | 2014-10-15 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420227877.XU Expired - Lifetime CN203874490U (en) | 2014-05-06 | 2014-05-06 | Ethanol distillation system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203874490U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109661259A (en) * | 2016-09-08 | 2019-04-19 | 伊士曼化工公司 | For separating the method for being thermally integrated Distallation systm and use it of the ternary composition with heterogeneous azeotrope |
| CN114225456A (en) * | 2021-12-23 | 2022-03-25 | 天津大学 | Novel separation device and separation method for coal-to-ethanol liquid-phase product |
| CN114470836A (en) * | 2021-12-28 | 2022-05-13 | 天津大学 | Separation device and separation method for coal-to-ethanol liquid-phase product based on ethyl acetate cutting |
-
2014
- 2014-05-06 CN CN201420227877.XU patent/CN203874490U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109661259A (en) * | 2016-09-08 | 2019-04-19 | 伊士曼化工公司 | For separating the method for being thermally integrated Distallation systm and use it of the ternary composition with heterogeneous azeotrope |
| CN109661259B (en) * | 2016-09-08 | 2021-10-01 | 伊士曼化工公司 | Heat integrated distillation system for separating ternary compositions with heterogeneous azeotropes and methods of using same |
| CN114225456A (en) * | 2021-12-23 | 2022-03-25 | 天津大学 | Novel separation device and separation method for coal-to-ethanol liquid-phase product |
| CN114225456B (en) * | 2021-12-23 | 2023-02-07 | 天津大学 | Separation device and separation method for coal-to-ethanol liquid-phase product |
| CN114470836A (en) * | 2021-12-28 | 2022-05-13 | 天津大学 | Separation device and separation method for coal-to-ethanol liquid-phase product based on ethyl acetate cutting |
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Legal Events
| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |